TEMA_EighthEdition

STANDARDS OF THE

TUBULAR EXCHANGER

MANUFACTURERS ASSOCIATION

EIGHTH EDITION

TUBULAR EXCHANGER MANUFACTURERS ASSOCIATION, INC. 25 North Broadway

Tarrytown, New York 10591 Richard C. Byrne, Secretary

www.tema.org

i

NO WARRANTY EXPRESSED OR IMPLIED

The Standards herein are recommended b The Tubular Exchanger Manufacturers Association, InC.

standards are based upon sound engineering principles, research and field experience in the manufacture, design, installation and use of tubular exchangers. These standards may be subject to revision as further investigation or experience may show is necessary or desirable. Nothing herein shall constitute a warranty of any kind, expressed or implied, and warranty responsibility of any kind is expressly denied.

to assist users, engineers and designers w Yl o specify, design and install tubular exchangers. These

0 Copyright 1968,1970,1972,1974,1978,1986,1987,1988, 1999 Tubular Exchanger Manufacturers Association, Inc.

TEMA is a trademark of the Tubular Exchanger Manufacturers Association, Inc.

This document may not be copied, photocopied, reproduced, translated, modified or reduced to any electronic medium or machine-readable form in whole or in part, without prior written consent of the Tubular Exchanger Manufacturers Association, Inc.

ALL RIGHTS RESERVED

ii

CONTRIBUTING MEMBERS TUBULAR EXCHANGER MANUFACTURERS ASSOCIATION, INC.

Comprising Manufacturers of Various Types of Shell and Tube Heat Exchanger Equipment

API Heat Transfer, Inc. ................................................................................ 2777 Walden Avenue Buffalo, NY 14225

Cust-O-Fab, lnc .......................................................................................... 8888 West 21 st Street Sand Springs, OK 74063

Energy Exchanger Company .................................................................... 1844 N. Garnett Road

Engineers and Fabricators Company ...................................................... 3501 West 1 1 th Street

Tulsa, OK 741 16

Houston, TX 77008-6001 1

Fabsco Shell and Tube, LL.C .................................................................................. P.O. Box 988 Sapulpa, OK 74066

Graham Corporation ..................................................................................... 20 Florence Avenue Batavia, NY 14020

Heat Transfer Equipment Co ............................................................................. P.O. Box 580638

Hughes-Anderson Heat Exchangers, Inc ................................................ 1001 N. Fulton Avenue

Tulsa, OK 74158

Tulsa, OK 741 15

IlT Standard, ITT Fluid Technology Corporation ................................................ P.O. Box 1102 Buffalo, NY 14227

Joseph Oat Corporation ..................................................................................... 2500 Broadway Camden, NJ 08104

Manning and Lewis Engineering Company ................................................. 675 Rahway Avenue Union, NJ 07083

Nooter Corporation ................................................................................................. P.O. Box 451 St. Louis, MO 63166

Ohmstede, Inc ............................................................................................ 825 North Main Street Beaumont, TX 77701

RAS Process Equipment, Inc ................................................................ 324 Meadowbrook Road Robbinsville, NJ 08691

Southern Heat Exchanger Corporation ................................................................ P.O. Box 1850 Tuscaloosa, AL 35403

Struthers Industries, Inc ...................................................................................... 1500 34th Street Gulfport. MS 39501

Wiegmann and Rose ............................................................................................... 0. Box 4187 Oakland, CA 94614

Yuba Heat Transfer ............................................................................................... P.O. Box 3158 Tulsa, OK 74101

Subsidiary of Xchanger Mfg. Corp.

A Division of Connell Limited Partnership

iii

TECHNICAL COMMllTEE OF THE

TUBULAR EXCHANGER MANUFACTURERS ASSOCIATION

Ken O’Connor ......................................................................................... ..API Heat Transfer, Inc.

Doug Werhane .................................................................................................... Cust-0-Fab, Inc.

Ken Fultz ......................................................................................... Energy Exchanger Company

Cris Smelley ..................................................................... ..Engineers and Fabricators Company .. Philip Marks .................................................................................................. Graham Corporation

Monte Davis ......................................................................... Heat Transfer Equipment Company

Jim Harrison ............................................................... Hughesanderson Heat Exchangers, Inc.

Nick Tranquilli ............................... ........................................................................ ITT Standard

Michael Holtz ........................................................................................ Joseph Oat Corporation

Steve Meierotto .............................................................................................. Nooter Corporation

Ted Rapczynski .................................................................. Manning and Lewis Engineering Co.

Michael Tracy ........................................................................................................ Ohmstede, Inc. Russell Miller

Dan-Skenman

Gary L. Berry .......................................................................................... Struthers Industries, Inc.

Subsidiary of Xchanger Mfg. Corp.

A Division of Connell Limited Partnership

Todd Allen ................................................................................. Southern Heat Exchanger Corp.

Jack E. Logan .............................................................................................. Wiegmann and Rose

Larry Brumbaugh ........................................................................................... Yuba Heat Transfer

iv

PREFACE

Eighth Edition - 1999

The Eighth Edition of the TEMA Standards was prepared by the Technical Committee of the Tubular Exchanger Manufacturers Association. A compilation of previously proven information, along with new additions to the Flow Induced Vibration, Flexible Shell Elements and Tubesheet Design sections is presented for your practical use. Design methods for Floating Head Backing Devices have also been added and the scope has been changed to accommodate a larger range of sizes and pressures. Metric units and tables have been included wherever possible. Suggested methods have been included for support and lifting lug design in the RGP section. This edition of the TEMA Standards is dedicated to the memory of Wayne Schaefer of the Nooter Corporation for his years of dedicated service to the TEMA Technical Committee. The Editor also wishes to acknowledge the contributions to the Eighth Edition by the following past members of the Technical Committee: Victor J. Stachura, Joseph H. Kissel, Robert C. Moscicki and Harry W. Saultz.

Jim Harrison EDITOR

V

CONTENTS

Section

1

2

3

4

5

6

Symbol & Parag rap h

G 1 2 3 4 5 6 7

E 1 2 3 4

RCB 1 2 3 4 5 6 7 8 9 10 11

V 1 2 3 4 5 6 7 8

... MEMBERSHIP LIST ............................................................................................................................... .I11

TECHNICAL COMMITTEE ..................................................................................................................... iv PREFACE ............................................................................................................................................... V

NOTES TO USERS ............................................................................................................................... Vlll

NOMENCLATURE Size Numbering and Type Designation-Recommended Practice .......................................................... 1 Nomenclature of Heat Exchanger Components ..................................................................................... 3

.................................................. 6

...

FAB RlCATlON TOLERANCES External Dimensions, Nozzle and Support Locations .... Recommended Fabrication Tolerances ................................ Tubesheets, Partitions, Covers, and Flanges ...................................... Flange Face Imperfections ..........................................

........................ ..................................... 9

GENERAL FABRICATION AND PERFORMANCE INFORMATION ..................................

.................................................. 13 Nameplates .............................................. ....................... .................................................. 13 Drawings and ASME Code Data Reports ..................... ................................................................ 13 Guarantees ........................................................................................................................................ f 4 Preparation of Heat Exchangers for Shipment ..................................................................................... 15 General Construction Features of TEMA Standard Heat Exchangers ................................................... 15

INSTALLATION, OPERATION, AND MAINTENANCE Performance of Heat Exchangers ........................................................................................... Installation of Heat Exchangers .................. Operation of Heat Exchangers ............................................................................................................ 18

..........................................................

Maintenance of Heat Exchangers ..........................................................

Scope and General Requirements ......................................................... Tubes ....... ......................................................... .............................................................. ...27 Shells and Shell Covers ............................ ............................................................................. .30 Baffles and Support Plates ........................ ............................................................ 31 Floating End Construction .................................................................................................................. 38 Gaskets ............................................................................................................................................. 43 Tubesheets ........................................................................................................................................ 45 Flexible Shell Elements 75

Channels, Covers, and Bonnets .......................................................................................................... 88 Nozzles .............................................................................................................................................. 91 End Flanges and Bolting ..................................................................................................................... 93

Scope and General ............................................................................................................................. 95 Vibration Damage Patterns ............................................................................................................... ..95 Failure Regions ................................................................................................................................. .95 Dimensionless Numbers .............................................................................................................

Axial Tube Stress ............................................................................................................................. 104

Damping .......................................................................................................................................... 107

...................................... 19

...................................... 23 MECHANICAL STANDARD TEMA CLASS RCB HEAT EXCHANGERS

......................................................................................................................

FLOW INDUCED VIBRATION

Natural Frequency ......................... ................................................................... 97

Effective Tube Mass ......................................................................................................................... 104

vi

CONTENTS

Symbol & Section Paragraph 0 6 V FLOW INDUCED VIBRATION (continued)

9 10

114 11 Vibration Amplitude .......................................................................................................................... 12 Acoustic Vibration ............................................................................................................................ 116

Shell Side Velocity Distribution ......................................................................................................... 109 Estimate of Critical Flow Velocity ...................................................................................................... 112

13 Design Considerations ..................................................................................................................... 121 14 Selected References ........................................................................................................................ 122

2 Fouling ............................................................................................................................................. 125 3 Fluid Temperature Relations ............................................................................................. 126

1 Fluid Density ...................... .................................................................................................... 150 2 Specific Heat ............ ................................................................................................................ 150

Heat Content of Petroleum Fractions ................................................................................................ 151

5 Viscosity ............. ................................ ................................................................................ 151 6 Critical Properties ............................................................................................................................. 152

Properties of Gas and Vapor Mixtures ............................................................................................... 152

7 T THERMAL RELATIONS ............................................................................................................... 1 Scope and Basic Relations 124

4 Mean Metal Temperatures o Tubes .......................................................................... 8 P PHYSICAL PROPERTIES OF FLUIDS

3 4 Thermal Conductivity ........................................................................................................................ 151

7 8 Selected References ........................................................................................................................ 153

183 GENERAL IN FO RM AT10 N

(See detailed Table of Contents) 0 9 D

....................................................................................................... 10 RGP RECOMMENDED GOOD PRACTICE

G-7.11 G-7.12

Horizontal Vessel Supports ............................................................................................................... 253 Vertical Vessel Su~ports ................................................................................................................... 267

G-7.2 G-7.3 RCB-2 RCB-4 RCB-6 RCB-7 RCB-9 RCB-10 RCB-11 T-2

. . Lifting Lugs ...................................................................................................................................... 269 Wind and Seismic Design ................................................................................................................. 273 Plugging Tubes in Tube Bundle ........................................................................................................ 273 Entrance and Exit Areas ................................................................................................................... 274

Tubesheets ...................................................................................................................................... 279

Nozzles ............................................................................................................................................ 281

INDEX ................................................................................................................................................. 291

Gaskets ........................................................................................................................................... 279

Channels, Covers, and Bonnets ........................................................................................................ 280

End Flanges and Bolting ................................................................................................................... 281 Fouling ............................................................................................................................................. 283

vii

NOTES TO USERS OF

THE TEMA STANDARDS

Three classes of Mechanical Standards, R,C and B, reflecting acceptable designs for various service applications are presented. The user should refer to the definition of each class and choose the one that best fits the specific need.

Corresponding subject matter in the three Mechanical Standards is covered by paragraphs identically numbered except for the prefix letter. Paragraph numbers preceded by RCB indicates that all three classes are identical. Any reference to a specific paragraph must be preceded by the class designation.

The Recommended Good Practice section has been prepared to assist the designer in areas outside the scope of the basic Standards. Paragraphs in the Standards having additional information in the RGP section are marked with an asterisk (*). The reference paragraph in the RGP section has the identical paragraph number, but with an "RGP" prefix.

It is the intention of the Tubular Exchanger Manufacturers Association that this edition of its Standards may be used beginning with the date of issuance, and that its requirements supersede those of the previous edition six months from such date of issuance, except for 'heat exchangers contracted for prior to the end of the six month period. For this purpose the date of issuance is June 1, 1999.

Questions on interpretation of the TEMA Standards should be formally addressed to the Secretary at TEMA 25 North Broadway, Tarrytown, NY 10591. Questions requiring development of new or revised technical information will only be answered through an addendum or a new edition of the Standards.

Upon agreement between purchaser and fabricator, exceptions to TEMA requirements are acceptable. An exchanger may still be considered as meeting TEMA requirements as long as the exception is documented.

viii

HEAT EXCHANGER NOMENCLATURE SECTION 1

N-1 SIZE NUMBERING AND TYPE DESIGNATION--RECOMMENDED PRACTICE It is recommended that heat exchanger size and type be designated by numbers and letters as described below.

0 N-1.1 SIZE

Sizes of shells (and tube bundles) shall be designated by numbers describing shell (and tube bundle) diameters and tube lengths, as follows:

N-1 .I 1 NOMINAL DIAMETER The nominal diameter shall be the inside diameter of the shell in inches (mm), rounded off to the nearest integer. For kettle reboilers the nominal diameter shall be the port diameter followed by the shell diameter, each rounded off to the nearest integer.

The nominal length shall be the tube length in inches (mm). Tube length for straight tubes shall be taken as the actual overall length. For U-tubes the length shall be taken as the approximate straight length from end of tube to bend tangent.

N-1.12 NOMINAL LENGTH

N-1.2 TYPE Type designation shall be by letters describing stationary head, shell (omitted for bundles only), and rear head, in that order, as indicated in Figure N-1.2.

N-1.3 NPICAL EXAMPLES

N-1.31 Split-ring floating head exchanger with removable channel and cover, single pass shell, 23-1 /4" (591 mm) inside diameter with tubes 16'(4877 mm) long. SIZE 23-1 92 (591 -4877) TYPE AES.

N-1.32 U-tube exchanger with bonnet type stationary head, split flow shell, 19" (483 mm) inside diameter with tubes 7'(2134 mm) straight length. SIZE 19-84 (483-2134) TYPE BGU.

N-1.33 Pull-through floating head kettle type reboiler having stationary head integral with tubesheet, 23" (584 rnm) port diameter and 37" (940 mm) inside shell diameter with tubes 16'(4877 rnm) long. SIZE 23137-192 (584,440 - 4877) TYPE CKT.

N-1.34 Fixed tubesheet exchanaer with removable channel and cover. bonnet t w e rear head. two pass shell, 33-1 8" (841 km) inside diameter with tubes 8'(2438 mm) long. SIZE 33-96 (841 -2438) TYP 6 AFM.

N-1.35 Fixed tubesheet exchanger having stationary and rear heads integral with tubesheets, single pass shell, 17" (432 mm) inside diameter with tubes 16'(4877 mrn) long. SIZE 17-192 (432-4877) TYPE NEN.

N-1.4 SPECIAL DESIGNS Special designs are not covered and may be described as best suits the manufacturer. For example, a single tube pass, fixed tubesheet exchanger with conical heads may be described as "TYPE BEM with Conical Heads". A pull-through floating head exchanger with an integral shell cover may be described as "TYPE AET with Integral Shell Cover".

Standards Of The Tubular Exchanger Manufacturers Association 1

SECTION 1

A

B

2

~ CHANNEL 1.1 A N D REMOVABLE COVER

HEAT EXCHANGER NOMENCLATURE

FRONT END

STATIONARY HEAD TYW

C5-5, BONNET (INTEGRAL COVER)

2i-b - CHANNEL INTEGRAL WITH TUBE

N

CHANNEL INTEGRAL WITH TUBE SHEET AND REMOVABLE COVER

SPECIAL HIGH PRESSURE CLOSUR

FIGURE N-1.2

SHEU TYPES

O N E PASS SHELL

-T-

TWO PASS SHELL WITH LONGITUDINAL BAFFLE

SPLIT FLOW

DOUBLE SPLIT FLOW

DIVIDED FLOW

T

I I

KEl lLE TYPE REBOILER

T

I

CROSS F L O W

FIXED TUBESHEET

FIXED TUBESHEET I LIKE "B" STATIONARY HEAD

N FIXED TUBESHEET I LIKE 'N" STATIONARY HEAD

OUTSIDE PACKED FLOATING H U I

FLOATING HEAD WITH B A C K I N G DEVICE

I PULL THROUGH FLOATING HEAD

U

U-TUBE BUNDLE

~- EXTERNALLY SEALED I FLOATING TUBESHEET

Stmciartds Of The Tubular Exchanger Manufacturers Association

HEAT EXCHANGER NOMENCLATURE SECTION 1

N-2 NOMENCLATURE OF HEAT EXCHANGER COMPONENTS For the purpose of establishing standard terminology, Figure N-2 illustrates various types of heat exchangers. Typical parts and connections, for illustrative purposes only, are numbered for identification in Table N-2.

0 1. 2. 3. 4. 5. 6. 7. 8. 9.

10. 11. 12. 13. 14. 15. 16. 17. 18. 19. 20.

TABLE N-2 Stationary Head-Channel Stationary Head-Bonnet Stationa Head Flange-Channel or Bonnet 23. Packing Box

21. Floating Head Cover-External 22. Floating Tubesheet Skirt

Channel x over Stationary Head Nozzle Stationary Tubesheet Tubes Shell Shell Cover Shell Flange-Stationary Head End Shell Flange-Rear Head End Shell Nozzle Shell Cover Flange Expansion Joint Floating Tubesheet Floating Head Cover Floating Head Cover Flange Floating Head Backing Device Split Shear Ring Slip-on Backing Flange

24. Packing 25. Packing Gland 26. Lantern Ring 27. Tierods and Spacers 28. Transverse Baffles or Support Plates 29. Impingement Plate 30. Longitudinal Baffle 31. Pass Partition 32. Vent Connection 33. Drain Connection 34. Instrument Connection 35. Support Saddle 36. Lifting Lug 37. Support Bracket 38. Weir 39. Liquid Level Connection 40. Floating Head Support

FIGURE N-2

AES


SECTION 1 HEAT EXCHANGER NOMENCLATURE

FIGURE N-2 (continued)

4

CFU

Standards Of The Tubular Exchanger Manufacturers Association

HEAT EXCHANGER NOMENCLATURE

FIGURE N-2 (continued)

SECTION 1

AKT

AJW


SECTION 2 HEAT EXCHANGER FABRICATION TOLERANCES

, . . 4

f1/4"(6.4) , f1/4"(6.4) fl/4"(6.4) f1/4"(6.4) f1/4"(6.4) I

I I -

I t

F-1 EXTERNAL DIMENSIONS, NOZZLE AND SUPPORT LOCATIONS Standard tolerances for process flow nozzles and support locations and projections are shown in Figure F-1 . Dimensions in ( ) are millimeters.

FIGURE F-1

f 1 /2"( 12.7) f 1 /4"(6.4) I

f1/4"(6.4) ~ I f 1/8"(3.2)

1 NOMINAL NOZZLE SIZE I G MAX

1 /4"(6.4) I NOTE: This toble ODOlieS to nozzles connecting to I I eifernol piping only. I

1 /8'(3.2) I f 1 /8'(3.2)/ 1 -

CONNECTION NOZZLE ALIGNMENT AND SUPPORT TOLERANCES

ALLOWABLE CENTERLINE ROTATION

STACKED EXCHANGERS

ROTATIONAL TOLERANCE ON NOZZLE FACES AT BOLT CIRCLE

6 Standards Of The Tubular Exchanger Manufacturers Association

HEAT EXCHANGER FABRICATION TOLERANCES SECTION 2

F-2 RECOMMENDED FABRICATION TOLERANCES Fabrication tolerances normally required to maintain process flow nozzle and support locations aye shown in Figure F-2. These tolerances may be adjusted as necessary to meet the tolerances shown in Figure F-1 . Dimensions in ( ) are millimeters.

FIGURE F-2


SECTION 2 HEAT EXCHANGER FABRICATION TOLERANCES

0 F-3 TUBESHEETS, PARTITIONS, COVERS AND FLANGES The standard clearances and tolerances applying to tubesheets, partitions, covers and flanges are shown in Figure F-3. Dimensions in ( ) are millimeters.

FIGURE F-3

t

w t

OD IF '5. 0 + II 0

0

STANDARD CONRNED JOINT CONSTRUCTION

ALTERNATE TONGUE AND GROOVE

JOINT

17- -

STANDARD UNCONRNED PWN FACE JOINT CONSTRUCTION

~

Q

1. SECTON 2 IS NOT INTENDED TO PROHIBIT UNMACHINED TUBESHEET FACES AND FIAT COVER FACES. THEREFORE NO PLUS TOLERANCE IS SHOWN ON R4.

2. NEGATNE TOLERANCES SHALL NOT BE DIMENSIONS TOLERANCES

A MUENSONS CAN LESS THAN THAT D1.02.03, 04, Ds. 06 f1/32' (iD.8) REWIRED W DESIGN CALCULATQNS.

t fl/16' (fl.6) 3. FOR PERIPHERAL GASKETS, *CONFINED'

+1/4' -1/8. (4.6-4 -3.2) CONSIRLIED TO MEAN THAT

MEANS 'CONFINED ON THE ODg. R. = 3/16. (4.8) to' -1f32' ( to -0.8) , -. . . . . Rz=1/4' (6.4) R3=1/4' (6.4) t1/32' -0' (t0.8 -0) R4 = 3/16' (4.8) w1 .wz.w3 f1/32' (iD.8)

4. DFJML~ ~pm AND 00 NOT -1/32' (-0.8) (SEE NOTE 1) PRECLUDE THE USE OF OTHER D E W S

VftKti ARE FUNCTOWY EOUNALENT.

5. FOR UNITS OVER 60' (1524) TO 100' (2540) DMETER. TOLERANCES INCREASED TO f 1 /16*( 1.6).

hD V K4Y BE


NPS

1 /2 3/4

1-1 /2

2-1 /2

1 1-1 /4

2

3 3-1 /2 4

5 6 8 10 12

14 16 18 20 24

NOTES:

HEAT EXCHANGER FABRICATION TOLERANCES

FIGURE F-4

PERMISSIBLE IMPERFECTIONS IN FLANGE FACING FINISH FOR RAISED FACE AND LARGE MALE AND FEMALE FLANGES l l 2

Maximum Radial Projection of Impedections Which Are No Deeper Than

the Bottom of the Serrations, in. (mm)

1/8 (3.2)

3/16 (4.8)

5/16 (7.9)

Maximum Depth and Radial Projection of Imperfections Which Are Deeper Than the

Bottom of the Serrations, in. (mm)

1/16 (1.6)

3/16 4.8

(1) Imperfections must be separated by at least four times the permissible radial projection. (2) Protrusions above the serrations are not permitted.

FLANGE PERIPHERY FLANGE PERIPHERY

(RAISED)

Sketch showing Radial Projected Length (RPL) serrated gasket face damage

SECTION 2


GENERAL FABRICATION AND PERFORMANCE INFORMATION SECTION 3

1.

2.

3.

4.

5.

6.

7.

8.

9.

10.

11.

12.

13.

14.

15.

16.

17.

18.

19.

20.

DEFINITIONS Baffie is a device to direct the shell side fluid across the tubes for optimum heat transfer. Baffle and Support Plate Tube Hole Clearance is the diametral difference between the nominal tube OD and the nominal tube hole diameter in the baffle or support plate. Consequential Damaaes are indirect liabilities lying outside the heat exchanger manufacturer’s stated equipment warranty obligations. Double Tubesheet Construction is a type of construction in which two (2) spaced tubesheets or equivalent are employed in lieu of the single tubesheet at one or both ends of the heat exchanger. Effective Shell and Tube Side Desian Pressures are the resultant load values expressed as uniform pressures used in the determination of tubesheet thickness for fixed tubesheet heat exchangers and are functions of the shell side design pressure, the tube side design pressure, the equivalent differential expansion pressure and the equivalent bolting pressure. Eauivalent Boltina Pressure is the pressure equivalent resulting from the effects of bolting loads imposed on tubesheets in a fixed tubesheet heat exchanger when the tubesheets are extended for bolting as flanged connections. Eauivalent Differential Exoansion Pressure is the pressure equivalent resulting from the effect of tubesheet loadings in a fixed tubesheet heat exchanger imposed by the restraint of differential thermal expansion between shell and tubes. Exoanded Tube Joint is the tube-to-tubesheet joint achieved by mechanical or explosive expansion of the tube into the tube hole in the tubesheet. ExDansion Joint ”J” Factor is the ratio of the spring rate of the expansion joint to the sum of the axial spring rate of the shell and the spring rate of the expansion joint. Flanae Load Concentration Factors are factors used to compensate for the uneven application of bolting moments due to large bolt spacing. Minimum and Maximum Baffle and Support Spacinas are design limitations for the spacing of.baffles toprovide for mechanical integrity and thermal and hydraulic effectiveness of the bundle. The posslbllity for induced vibration has not been considered in establishing these values. Normal Operatina Conditions of a shell and tube heat exchanger are the thermal and hydraulic performance requirements generally specified for sizing the heat exchanger. Pulsatina Fluid Conditions are conditions of flow generally characterized by rapid fluctuations in pressure and flow rate resulting from sources outside of the heat exchanger. Seismic Loadinas are forces and moments resulting in induced stresses on any member of a heat exchanger due to pulse mode or complex waveform accelerations to the heat exchanger, such as those resulting from earthquakes. Shell and Tube Mean Metal Temperatures are the average metal temperatures through the shell and tube thicknesses integrated over the length of the heat exchanger for a given steady state operating condltlon. Shut-Down Conditions are the conditions of operation which exist from the time of steady state operating conditions to the time that flow of both process streams has ceased. Start-Ur, Conditions are the conditions of operation which exist from the time that flow of either or both process streams is initiated to the time that steady state operating conditions are achieved. S u ~ ~ o r t plate is a device to support the bundle or to reduce unsupported tube span without consideration for heat transfer. Tubesheet Liaament is the shortest distance between edge of adjacent tube holes in the tube pattern. Welded Tube Joint is a tube-to-tubesheet joint where the tube is welded to the tubesheet.


0 1 2 3 4 5 6 7 8 9

10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60 61

0

Job No Customer Reference No Address Proposal No Plant Location Date Rev Service of Untt Item No

SurfIUnR (GrossIEff ) Sq Ft, ShellslUnR SurflShell (GrosslEff )

Fluid Allocation Shell Side Tube Side Fluid Name Fluid Quantity Total LblHr

(HorNert) Connected in Parallel Series Sq Ft

Sue Type

PERFORMANCE OF ONE UNIT

Vapor (Inlout) I I Liquid I I Steam I I Water I I Noncondensable I I

Temperature (Inlout) OF I I Specfic Gravity I I Viscosity, Liquid CP I I Molecular Weight, Vapor I I Molecular Weight, Noncondensable I I Specfic Heat Btu I Lb OF I I Thermal Conductivity Btu Ft I Hr Sq Ft OF I I Latent Heat Btu I Lb @ O F Inlet Pressure Psia Veloctty Ft I Sec

Fouling Resistance (Min ) Hi Sq Ft OF/ Btul

Transfer Rate, Service Clean

Pressure Drop, Allow ICalc PSI I I

Heat Exchanged Btu I Hr MTD (Corrected) OF Btu I Hr Sq Ft OF

CONSTRUCTION OF ONE SHELL Sketch (BundleINoule orientation) I Shell Side Tube Side

Design I Test Pressure Ps1g I I Design Temp. MaxlMin OF I I No Passes per Shell Corrosion Allowance In Connections In

Sue& Out Rating Intermediate

Tube No. OD In:Thk (MinlAvg) In,Length Ft.PRch In + m *(R)=90 +45 TubeType Matenal Shell ID OD In Shell Cover (Integ ) (Remov.) Channel or Bonnet Channel Cover TubesheetStationary Tubesheet-Floating Floating Head Cover Impingement Protection BafflesCross Type %Cut (DiamIArea) Spacing clc Inlet In Baffles-Long Seal Type Suppott~-Tube U-bnd Type Bypass Seal Arrangement Tube-to-Tubesheet Joint Expansion Joint Type pv'-Inlet Nozzle Bundle Entrance Bundle ExR GasketsShell Side Tube Side Floating Head Code Requirements TEMA Class Weight I Shell Remarks

Bundle Lb Filled wtth Water


FIGURE G-5.2 HEAT EXCHANGER SPECIFICATION SHEET


SECTION 3 GENERAL FABRICATION AND PERFORMANCE INFORMATION

1 2 3 4 5 6

8 9

10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49

51 52 53 54 55 56 57 58 ca

7

50

FIGURE G-5.2M HEAT EXCHANGER SPECIFICATION SHEET

Job No Customer Reference No Address Proposal No

Plant Location Date Rev Service of Unlt Item No Slze Type (HorNert) Connected in Parallel Series SurflUnit (GrosslEff) Sq m. ShellslUnlt SurflShell (GrosdEff ) Sq m

PERFORMANCE OF ONE UNIT Tube Side Fluid Allocation Shell Side

Fluid Name Fluid Quantity Total kglHr -

Vapor (Inlout) I I Liquid I I Steam I I

I Water I Noncondensable I I

Temperature (InlOut) OC I I Specific Gravity I I Viscosity, Liquid CP I I Molecular Weight, Vapor I I Molecular Weight. Noncondensable I I Specific Heat Jlkg OC I I Thermal Conductivity Wlm OC I I

-

Latent Heat Jlkg @ OC Inlet Pressure kPa(abs ) Veloctty mlsec

Fouling Resistance (Min ) Sqm OC/W

Transfer Rate, Service Clean W/Sq m OC

Shell Side Tube Side

Pressure Drop, Allow lCalc kPa I I

Heat Exchanged W MTD (Corrected) OC

CONSTRUCTION OF ONE SHELL Sketch (BundlelNoule Orientation)

Design I Test Pressure kPag I I DesignTemp Max/Min OC l I No PassesperShell Corrosion Allowance mm Connections In

Size8 Out Rating Intermediate

Tube No OD mm,Thk (MinlAvg) mm , Length mm,Pltch mm +30 -& 6 0 8 9 0 +45 TubeType Material Shell ID OD mm (Shell Cover (Integ ) (Remov Channel or Bonnet Channel Cover Tubesheet-Stationary Tubesheet-Floating Floating Head Cover Impingement Protection Baffles-Cross Type %Cut (DiamIArea) Spacing d c Inlet mn Baffles-Long Seal Type S~pports-T~be U-Bend Type Bypass Seal Arrangement Tube-to-Tubesheet Joint Expansion Joint Type p#-lnlet Nozzle Bundle Entrance Bundle Exlt Gaskets-Shell Side Tube Side Floating Head Code Requirements TEMA Class Weight I Shell Filled with Water Bundle kc Remarks

~

60 61



G-1 SHOP OPERATION The detailed methods of shop operation are left to the discretion of the manufacturer in conformity with these Standards.

G-2 INSPECTION

G-2.1 MANUFACTURER'S INSPECTION Inspection and testing of units will be provided by the manufacturer unless otherwise specified. The manufacturer shall carry out the inspections required by the ASME Code, and also inspections required by state and local codes when the purchaser specifies the plant location.

G-2.2 PURCHASER'S INSPECTION The purchaser shall have the right to make inspections during fabrication and to witness any tests when he has so requested. Advance notification shall be given as agreed between the manufacturer and the purchaser. Inspection by the purchaser shall not relieve the manufacturer of his responsibilities.

G-3 NAME PLATES

G-3.1 MANUFACTURER'S NAME PLATE A suitable manufacturer's name plate of corrosion resistant material shall be permanently attached to the head end or the shell of each TEMA exchanger. Name plates for exchangers manufactured in accordance with Classes "R" and "6" shall be austenitic (300 series) stainless. When insulation thickness is specified by the purchaser, the name plate shall be attached to a bracket welded to the exchanger.

G-3.11 NAME PLATE DATA In addition to all data required by the ASME Code, a name plate shall also include the following (if provided): User's equipment identification User's order number

G-3.12 SUPPLEMENTAL INFORMATION The manufacturer shall supply supplemental information where it is pertinent to the operation or testing of the exchanger. This would include information pertaining to differential design and test pressure conditions, restrictions on operating conditions for fixed tubesheet type exchangers, or other restrictive conditions applicable to the design and/or operation of the unit or its components. Such information can be noted on the name plate or on a supplemental plate attached to the exchanger at the name plate location.

G-3.2 PURCHASER'S NAME PLATE Purchaser's name plates, when used, are to be supplied by the purchaser and supplement rather than replace the manufacturer's name plate.

G-3.3 TEMA REGISTRATION PLATE The TEMA organization has adopted a voluntary registration system for TEMA members only. When a heat exchanger is registered with TEMA, a unique number is assigned to the heat exchanger. A TEMA registration plate, showing this number, is affixed to the heat exchanger and the ASME Code data report is placed on file at the TEMA office. By referencing this registration number, a copy of the ASME Code data report may be obtained by the purchaser from the TEMA office.

G-4 DRAWINGS AND ASME CODE DATA REPORTS

G-4.1 DRAWINGS FOR APPROVAL AND CHANGE The manufacturer shall submit for purchaser's approval three (3) prints of an outline drawing showing nozzle sizes and locations, overall dimensions, supports and weight. Other drawings may be furnished as agreed upon by the purchaser and the manufacturer. It is anticipated that a reasonable number of minor drawing changes may be required at that time. Changes subsequent to receipt of approval may cause additional expense chargeable to the purchaser. Purchaser's approval of drawings does not relieve the manufacturer of responsibility for compliance with this Standard and applicable ASME Code requirements. The manufacturer shall not make any changes



on the approved drawings without express agreement of the purchaser. Shop detail drawings, while primarily for internal use by the fabricator, may be furnished to the purchaser upon request. When detail drawings are requested, they will only be supplied after outline drawings have been approved.

G-4.2 DRAWINGS FOR RECORD After approval of drawings, the manufacturer shall furnish three (3) prints or, at his option, a transparency of all approved drawings.

The drawings and the design indicated by them are to be considered the property of the manufacturer and are not to be used or reproduced without his permission, except by the purchaser for his own internal use.

G-4.3 PROPRIETARY RIGHTS TO DRAWINGS

G-4.4 ASME CODE DATA REPORTS After completion of fabrication and inspection of ASME Code stamped exchangers, the manufacturer shall furnish three (3) copies of the ASME Manufacturer’s Data Report.

G-5 GUARANTEES

G-5.1 GENERAL The specific terms of the guarantees should be agreed upon by the manufacturer and purchaser. Unless otherwise agreed upon by the manufacturer and purchaser, the following paragraphs in this section will be applicable.

G-5.2 PERFORMANCE The purchaser shall furnish the manufacturer with all information needed for clear understanding of performance requirements, including any special requirements. The manufacturer shall guarantee thermal performance and mechanical design of a heat exchanger, when operated at the design conditions specified by the purchaser in his order, or shown on the exchanger specification sheet furnished by the manufacturer (Figure G-5.2, G-5.2M). This guarantee shall extend for a period of twelve (1 2) months after shipping date. The manufacturer shall assume no responsibility for excessive fouling of the apparatus by material such as coke, silt, scale, or any foreign substance that may be deposited. The thermal guarantee shall not be applicable to exchangers where the thermal performance rating was made by the purchaser.

G-5.21 THERMAL PERFORMANCE TEST A performance test shall be made if it is established after operation that the performance of the exchanger is not satisfactory, provided the thermal performance rating was made by the manufacturer. Test conditions and procedures shall be selected by agreement between the purchaser and the manufacturer to permit extrapolation of the test results to the specified design conditions.

The manufacturer shall repair or replace F.O.B. his plant any parts proven defective within the guarantee period. Finished materials and accessories purchased from other manufacturers, including tubes, are warranted only to the extent of the original manufacturer’s warranty to the heat exchanger fabricator.

G-5.22 DEFECTIVE PARTS

G-5.3 CONSEQUENTIAL DAMAGES The manufacturer shall not be held liable for any indirect or consequential damage.

G-5.4 CORROSION AND VIBRATION The manufacturer assumes no responsibility for deterioration of any part or parts of the equipment due to corrosion, erosion, flow induced tube vibration, or any other causes, regardless of when such deterioration occurs after leaving the manufacturer’s premises, except as provided for in Paragraphs G-5.2 and (3-5.22.



G-5.5 REPLACEMENT AND SPARE PARTS When replacement or spare tube bundles, shells, or other parts are purchased, the manufacturer is to guarantee satisfactory fit of such parts only if he was the original manufacturer. Parts fabricated to drawings furnished by the purchaser shall be guaranteed to meet the dimensions and tolerances specified.

0 G-6 PREPARATION OF HEAT EXCHANGERS FOR SHIPMENT

G-6.1 CLEANING Internal and external surfaces are to be free from loose scale and other foreign material that is readily removable by hand or power brushing.

Water, oil, or other liquids used for cleaning or hydrostatic testing are to be drained from all units before shipment. This is not to imply that the units must be completely dry.

G-6.2 DRAINING

G-6.3 FLANGE PROTECTION All exposed machined contact surfaces shall be coated with a removable rust preventative and protected against mechanical damage by suitable covers.

G-6.4 THREADED CONNECTION PROTECTION All threaded connections are to be suitably plugged.

G-6.5 DAMAGE PROTECTION The exchanger and any spare parts are to be suitably protected to prevent damage during shipment.

G-6.6 EXPANSION JOINT PROTECTION External thin walled expansion bellows shall be equipped with a protective cover which does not restrain movement. 0 G-7 GENERAL CONSTRUCTION FEATURES OF TEMA STANDARD HEAT EXCHANGERS

G-7.1 SUPPORTS All heat exchangers are to be provided with supports.

*G-7.11 HORIZONTAL UNITS The supports should be designed to accommodate the weight of the unit and contents, including the flooded weight during hydrostatic test. For units with removable tube bundles, supports should be designed to withstand a pulling force equal to 1-1 /2 times the weight of the tube bundle. For purposes of support design, forces from external nozzle loadings, wind and seismic events are assumed to be negligible unless the purchaser specifically details the requirements. When these additional loads and forces are required to be considered, the combinations need not be assumed to occur simultaneously. The references under Paragraph G-7.13 may be used for calculating resulting stresses due to the saddle supports. Horizontal units are normally provided with at least two saddle type supports, with holes for anchor bolts. The holes in all but one of the supports are to be elongated to accommodate axial movement of the unit under operating conditions. Other types of support may be used if all design criteria are met, and axial movement is accommodated.

Vertical units are to be provided with supports adequate to meet design requirements. The supports may be of the lug, annular ring, leg or skirt type. If the unit is to be located in a supporting structure, the supports should be of sufficient size to allow clearance for the body flanges.

*G-7.12 VERTICAL UNITS



G-7.13 REFERENCES (1) Zick, L. P., "Stresses in Large Horizontal Cylindrical Pressure Vessels on Two Saddle

(2) Vinet, R., and Dore, R., "Stresses and Deformations in a Cylindrical Shell Lying on a

(3) Krupka, V., "An Analysis for Lug or Saddle Supported Cylindrical Pressure Vessels,"

Supports," Pressure Vessel and Piping; Design and Analysis, ASME, 1972.

Continuous Rigid Support," Paper No. 75-AM-1, Journal of Applied Mechanics, Trans. ASME.

Proceedings of the First International Conference on Pressure Vessel Technology, pp.

(4) Singh, K. P., Soler, A. I . , "Mechanical Design of Heat Exchangers and Pressure Vessel

(5) Bijlaard, P. P., "Stresses from Local Loadings in Cylindrical Pressure Vessels," Trans. ASME,

(6) Wichman, K. R., Hopper, A. G., and Mershon, J. L., "Local Stresses in Spherical and

491 -500.

Components," Chapter 17, Arcturus Publishers, Inc.

Vol. 77, No. 6, (August 1955).

Cylindrical Shells due to External Loadings," Welding Research Council, Bulletin No. 107, Rev. 1.

Piping Systems," Welding Research Council Bulletin No. 198. (7) Rodabaugh, E. C., Dodge, W. G., and Moore, S. E., "Stress Indices at Lug Supports on

(8) Brownell, L. E., and Young, E. H., "Process Equipment Design," John Wiley & Sons Inc. (9) Jawad, M. H., and Farr, J. R., "Structural Analysis and Design of Process Equipment," John

Wiley and Sons, Inc., 1984. (1 0) Bednar, H. H., "Pressure Vessel Design Handbook," Van Nostrand Reinhold Company. (1 1) Blodgett, 0. W., "Design of Welded Structures," The James F. Lincoln Arc Welding

(12) Moss, Dennis R., "Pressure Vessel Design Manual," 1987, Gulf Publishing Company. Foundation, 1966.

*G-7.2 LIFTING DEVICES Channels, bonnets, and covers which weigh over 60 Ibs. (27.2 Kg) are to be provided with lifting lugs, rings or tapped holes for eyebolts. Unless otherwise specified, these lifting devices are designed to lift only the component to which they are directly attached. Lugs for lifting the complete unit are not normally provided. When lifting lugs or trunnions are required by the purchaser to lift the complete unit, the device must be adequately designed. (1) The purchaser shall inform the manufacturer about the way in which the lifting device will be used.

The purchaser shall be notified of any limitations of the lifting device relating to design or method of rigging.

(2) Liquid penetrant examination of the lifting device attachment weld should be considered on large heavy units.

(3) The design load shall incorporate an appropriate impact factor. (4) Plate-type lifting lugs should be oriented to minimize bending stresses. (5) The hole diameter in the lifting device must be large enough to accept a shackle pin having a load

rating greater than the design load. (6) The effect on the unit component to which the lifting device is attached should be considered. It

may be necessary to add a reinforcing plate, annular ring or pad to distribute the load. (7) The adequacy of the exchanger to accommodate the lifting loads should be evaluated.

For wind and seismic forces to be considered in the design of a heat exchanger, the purchaser must specify in the inquiry the design requirements. The "Recommended Good Practice" section of these Standards provides the designer with a discussion on this subject and selected references for design application.

*G-7.3 WIND & SEISMIC DESIGN


INSTALLATION, OPERATION AND MAINTENANCE SECTION 4

E-1 PERFORMANCE OF HEAT EXCHANGERS Satisfactory operation of heat exchangers can be obtained only from units which are properly designed and have built-in quality. Correct installation and preventive maintenance are user responsibilities.

E-1.1 PERFORMANCE FAILURES The failure of heat exchanger equipment to perform satisfactorily may be caused by one or more factors, such as: (1) Excessive fouling. (2) Air or gas binding resulting from improper piping installation or lack of suitable vents. (3) Operating conditions differing from design conditions. (4) Maldistribution of flow in the unit. (5) Excessive clearances between the baffles and shell and/or tubes, due to corrosion. (6) Improper thermal design. The user’s best assurance of satisfactory performance lies in dependence upon manufacturers competent in the design and fabrication of heat transfer equipment.

E-2 INSTALLATION OF HEAT EXCHANGERS

E-2.1 HEAT EXCHANGER SETTINGS

E-2.11 CLEARANCE FOR DISMANTLING For straight tube exchangers fitted with removable bundles, provide sufficient clearance at the stationary head end to permit removal of the bundle from the shell and provide adequate space beyond the rear head to permit removal of the shell cover and/or floating head cover. For fixed tubesheet exchangers, provide sufficient clearance at one end to permit withdrawal and replacement of the tubes, and enough space beyond the head at the opposite end to permit removal of the bonnet or channel cover. For U-tube heat exchangers, provide sufficient clearance at the stationary head end to permit withdrawal of the tube bundle, or at the opposite end to permit removal of the shell.

E-2.12 FOUNDATIONS Foundations must be adequate so that exchangers will not settle and impose excessive strains on the exchanger. Foundation bolts should be set to allow for setting inaccuracies. In concrete footings, pipe sleeves at least one size larger than bolt diameter slipped over the bolt and cast in place are best for this purpose, as they allow the bolt center to be adjusted after the foundation has set.

E-2.13 FOUNDATION BOLTS Foundation bolts should be loosened at one end of the unit to allow free expansion of shells. Slotted holes in supports are provided for this purpose.

E-2.14 LEVELING Exchangers must be set level and square so that pipe connections may be made without forcing.

E-2.2 CLEANLINESS PROVISIONS

E-2.21 CONNECTION PROTECTORS All exchanger openings should be inspected for foreign material. Protective plugs and covers should not be removed until just prior to installation.

The entire system should be clean before starting operation. Under some conditions, the use of strainers in the piping may be required.

E-2.22 DIRT REMOVAL


SECTION 4 INSTALLATION, OPERATION AND MAINTENANCE

E-2.23 CLEANING FACILITIES Convenient means should be provided for cleaning the unit as suggested under "Maintenance of Heat Exchangers," Paragraph E-4.

E-2.3 FITTINGS AND PIPING

E-2.31 BY-PASS VALVES It may be desirable for purchaser to provide valves and by-passes in the piping system to permit inspection and repairs.

When not integral with the exchanger nozzles, thermometer well and pressure gage connections should be installed close to the exchanger in the inlet and outlet piping.

E-2.32 TEST CONNECTIONS

E-2.33 VENTS Vent valves should be provided by purchaser so units can be purged to prevent vapor or gas binding. Special consideration must be given to discharge of hazardous or toxic fluids.

Drains may discharge to atmosphere, if permissible, or into a vessel at lower pressure. They should not be piped to a common closed manifold.

E-2.34 DRAINS

E-2.35 PULSATION AND VIBRATION In all installations, care should be taken to eliminate or minimize transmission of fluid pulsations and mechanical vibrations to the heat exchangers.

E-2.36 SAFETY RELIEF DEVICES The ASME Code defines the requirements for safety relief devices. When specified by the purchaser, the manufacturer will provide the necessary connections for the safety relief devices. The size and type of the required connections will be specified by the purchaser. The purchaser will provide and install the required relief devices.

E-3 OPERATION OF HEAT EXCHANGERS

E-3.1 DESIGN AND OPERATING CONDITIONS Equipment must not be operated at conditions which exceed those specified on the name plate@).

Before placing any exchanger in operation, reference should be made to the exchanger drawings, specification sheet@) and name plate(s) for any special instructions. Local safety and health regulations must be considered. Improper start-up or shutdown sequences, particularly of fixed tubesheet units, may cause leaking of tube-to-tubesheet and/or bolted flanged joints.

E-3.2 OPERATING PROCEDURES

E-3.21 START-UP OPERATION Most exchangers with removable tube bundles may be placed in service by first establishing circulation of the cold medium, followed by the gradual introduction of the hot medium. During start-up all vent valves should be opened and left open until all passages have been purged of air and are completely filled with fluid. For fixed tubesheet exchangers, fluids must be introduced in a manner to minimize differential expansion between the shell and tubes.

E-3.22 SHUT-DOWN OPERATION For exchangers with removable bundles, the units may be shut down by first gradually stopping the flow of the hot medium and then stopping the flow of the cold medium. If it is necessary to stop the flow of cold medium, the circulation of hot medium through the exchanger should also be stopped. For fixed tubesheet exchangers, the unit must be shut . down in a manner to minimize differential expansion between shell and tubes. When shutting down the system, all units should be drained completely when there is the possibility of freezing or corrosion damage. To guard against water hammer, condensate should be



drained from steam heaters and similar apparatus during start-up or shut-down. To reduce water retention after drainage, the tube side of water cooled exchangers should be blown out with air.

E-3.23 TEMPERATURE SHOCKS Exchangers normally should not be subjected to abrupt temperature fluctuations. Hot fluid must not be suddenly introduced when the unit is cold, nor cold fluid suddenly introduced when the unit is hot.

E-3.24 BOLTED JOINTS Heat exchangers are pressure tested before leaving the manufacturer’s shop in accordance with ASME Code requirements. However, normal relaxing of the gasketed joints may occur in the interval between testing in the manufacturer’s shop and installation at the jobsite. Therefore, all external bolted joints may require retightening after installation and, if necessary, after the exchanger has reached operating temperature.

It is important that all bolted joints be tightened uniformly and in a diametrically staggered pattern, as illustrated in Figure E-3.25, except for special high pressure closures when the instructions of the manufacturer should be followed.

E-3.25 RECOMMENDED BOLT TIGHTENING PROCEDURE

FIGURE E-3.25

START ’ I I 16

E-4 MAINTENANCE OF HEAT EXCHANGERS

E-4.1 INSPECTION OF UNIT At regular intervals and as frequently as experience indicates, an examination should be made of the interior and exterior condition of the unit. Neglect in keeping all tubes clean may result in comp!ete stoppage of flow through some tubes which could cause severe thermal strains, leaking tube joints, or structural damage to other components. Sacrificial anodes, when provided, should be inspected to determine whether they should be cleaned or replaced.

E-4.11 INDICATIONS OF FOULING Exchangers subject to fouling or scaling should be cleaned periodically. A light sludge or scale coating on the tube greatly reduces its efficiency. A marked increase in pressure drop and/or reduction in performance usually indicates cleaning is necessary. The unit should first be checked for air or vapor binding to confirm that this is not the cause for the reduction in performance. Since the difficulty of cleaning increases rapidly as the scale thickness or deposit increases, the intervals between cleanings should not be excessive.



20

E-4.12 DISASSEMBLY FOR INSPECTION OR CLEANING Before disassembly, the user must assure himself that the unit has been depressurized, vented and drained, neutralized and/or purged of hazardous material. To inspect the inside of the tubes and also make them accessible for cleaning, the following procedures should be used: (1) Stationary Head End

(a) Type A, C, D & N, remove cover only (b) Type B, remove bonnet

(a) Type L, N & P, remove cover only (b) Type M, remove bonnet (c) Type S & T, remove shell cover and floating head cover (d) Type W, remove channel cover or bonnet

(2) Rear Head End

E-4.13 LOCATING TUBE LEAKS The following procedures may be used to locate perforated or split tubes and leaking joints between tubes and tubesheets. In most cases, the entire front face of each tubesheet will be accessible for inspection. The point where water escapes indicates a defective tube or tube-to-tubesheet joint. (1) Units with removable channel cover: Remove channel cover and apply hydraulic pressure

in the shell. (2) Units with bonnet type head: For fixed tubesheet units where tubesheets are an integral

part of the shell, remove bonnet and apply hydraulic pressure in the shell. For fixed tubesheet units where tubesheets are not an integral part of the shell and for units with removable bundles, remove bonnet, re-bolt tubesheet to shell or install test flange or gland, whichever is applicable, and apply hydraulic pressure in the shell. See Figure E-4.13-1 for typical test flange and test gland.

FIGURE E-4.13-1

n isi

(3) Units with Type S or T floating head: Remove channel cover or bonnet, shell cover and floating head cover. Install test ring and bolt in place with gasket and packing. Apply hydraulic pressure in the shell. A typical test ring is shown in Figure E-4.13-2. When a test ring is not available it is possible to locate leaks in the floating head end by removing the shell cover and applying hydraulic pressure in the tubes. Leaking tube joints may then be located by sighting through the tube lanes. Care must be exercised when testing, partially assembled exchangers to prevent over extension of expansion joints or overloadlng of tubes and/or tube-to-tubesheet joints.

(4) Hydrostatic test should be performed so that the temperature of the metal is over 60" F (1 6" C) unless the materials of construction have a lower nilductility transition temperature.

Standards Of The-Tubular Exchanger Manufacturers Association


FLOATING

PACKING

FIGURE E-4.13-2

FLANGE- REAR HEAD END

E-4.2 TUBE BUNDLE REMOVAL AND HANDLING To avoid possible damage during removal of a tube bundle from a shell, a pulling device should be attached to eyebolts screwed into the tubesheet. If the tubesheet does not have tapped holes for eyebolts, steel rods or cables inserted through tubes and attached to bearing plates may be used. The bundle should be supported on the tube baffles, supports or tubesheets to prevent damage to the tubes. Gasket and packing contact surfaces should be protected.

E-4.3 CLEANING TUBE BUNDLES

E-4.31 CLEANING METHODS The heat transfer surfaces of heat exchangers should be kept reasonably clean to assure satisfactory performance. Convenient means for cleaning should be made available. Heat exchangers may be cleaned by either chemical or mechanical methods. The method selected must be the choice of the operator of the plant and will depend on the type of deposit and the facilities available in the plant. Following are several cleaning procedures that may be considered: (1) Circulating hot wash oil or light distillate through tubes or shell at high velocity may

(2) Some salt deposits may be washed out by circulating hot fresh water. (3) Commercial cleaning compounds are available for removing sludge or scale provided hot

wash oil or water is not available or does not give satisfactory results. (4) High pressure water jet cleaning. (5) Scrapers, rotating wire brushes, and other mechanical means for removing hard scale,

effectively remove sludge or similar soft deposits.

coke, or other deposits.



22

(6) Employ services of a qualified organization that provides cleaning services. These organizations will check the nature of the deposits to be removed, furnish proper solvents and/or acid solutions containing inhibitors, and provide equipment and personnel for a complete cleaning job.

E-4.32 CLEANING PRECAUTIONS (1) Tubes should not be cleaned by blowing steam through individual tubes since this heats

the tube and may result in severe expansion strain, deformation of the tube, or loosening of the tube-to-tubesheet joint.

(2) When mechanically cleaning a tube bundle, care should be exercised to avoid damaging the tubes.

(3) Cleaning compounds must be compatible with the metallurgy of the exchanger.

E-4.4 TUBE EXPANDING A suitable tube expander should be used to tighten a leaking tube joint. Care should be taken to ensure that tubes are not over expanded.

E-4.5 GASKET REPLACEMENT Gaskets and gasket surfaces should be thoroughly cleaned and should be free of scratches and other defects. Gaskets should be properly positioned before attempting to retighten bolts. It is recommended that when a heat exchanger is dismantled for any cause, it be reassembled with new gaskets. This will tend to prevent future leaks and/or damage to the gasket seating surfaces of the heat exchanger. Composition gaskets become dried out and brittle so that they do not always provide an effective seal when reused. Metal or metal jacketed gaskets, when compressed initially, flow to match their contact surfaces. In so doing they are work hardened and, if reused, may provide an imperfect seal or result in deformation and damage to the gasket contact surfaces of the exchanger. Bolted joints and flanges are designed for use with the particular type of gasket specified. Substitution of a gasket of different construction or improper dimensions may result in leakage and damage to gasket surfaces. Therefore, any gasket substitutions should be of compatible design. Any leakage at a gasketed joint should be rectified and not permitted to persist as it may result in damage to the gasket surfaces. Metal jacketed type gaskets are widely used. When these are used with a tongue and groove joint without a nubbin, the gasket should be installed so that the tongue bears on the seamless side of the gasket jacket. When a nubbin is used, the nubbin should bear on the seamless side.

E-4.6 SPARE AND REPLACEMENT PARTS The procurement of spare or re lacement parts from the manufacturer will be facilitated if the correct name for the part, as shown in 8 ection 1, Table N-2, of these Standards is given, together with the serial number, type, size, and other information from the name plate. Replacement parts should be purchased from the original manufacturer.

E-4.7 PLUGGING OF TUBES In U-tube heat exchangers, and other exchangers of special design, it may not be feasible to remove and replace defective tubes. Defective tubes may be plugged using commercially available tapered plugs with ferrules or tapered only plugs which may or may not be seal welded. Excessive tube plugging may result in reduced thermal performance, higher pressure drop, and/or mechanical damage. It is the user’s responsibility to remove plugs and neutralize the bundle prior to sending it to a shop for repairs.


SECTION 5 MECHANICAL STANDARDS TEMA CLASS R C B

RCB-1 SCOPE AND GENERAL REQUIREMENTS

RCB-1.1 SCOPE OF STANDARDS

RCB-1.11 GENERAL The TEMA Mechanical Standards are applicable to shell and tube heat exchangers which do not exceed any of the following criteria: (1) inside diameters of 100 inches (2540 mm) (2) product of nominal diameter, inches (mm) and design pressure, psi (kPa) of 100,000

(17.5 X lo6) (3) a design pressure of 3,000 psi (20684 kPa) The intent of these parameters is to limit the maximum shell wall thickness to approximately 3 inches (76 mm), and the maximum stud diameter to approximately 4 inches (102 mm). Criteria contained in these Standards may be applied to units which exceed the above parameters.

R-1.12 DEFINITION OF TEMA CLASS "R" EXCHANGERS The TEMA Mechanical Standards for Class "R" heat exchangers specify design and fabrication of unfired shell and tube heat exchangers for the generally severe requirements of petroleum and related processing applications.

The TEMA Mechanical Standards for Class " C heat exchangers specify design and fabrication of unfired shell and tube heat exchangers for the generally moderate requirements of commercial and general process applications.

The TEMA Mechanical Standards for Class " B heat exchangers specify design and fabrication of unfired shell and tube heat exchangers for chemical process service.

C-1.12 DEFINITION OF TEMA CLASS "C" EXCHANGERS

8-1.12 DEFINITION OF TEMA CLASS "B" EXCHANGERS

RCB-1.13 CONSTRUCTION CODES The individual vessels shall comply with the ASME (American Society of Mechanical Engineers) Boiler and Pressure Vessel Code, Section VIII, Division 1, hereinafter referred to as the Code. These Standards supplement and define the Code for heat exchanger applications. The manufacturer shall comply with the construction requirements of state and local codes when the purchaser specifies the plant location. It shall be the responsibility of the purchaser to inform the manufacturer of any applicable local codes. Application of the Code symbol is required, unless otherwise specified by the purchaser.

For purposes of these Standards, "carbon steel" shall be construed as any steel or low alloy falling within the scope of Part UCS of the Code. Metals not included by the foregoing (except cast iron) shall be considered as "alloys" unless otherwise specifically named. Materials of construction, including gaskets, should be specified by the purchaser. The manufacturer assumes no responsibility for deterioration of parts for any reason.

RCB-1.14 MATERIALS-DEFINITION OF TERMS

RCB-1.2 DESIGN PRESSURE

RCB-1.21 DESIGN PRESSURE Design pressures for the shell and tube sides shall be specified separately by the purchaser.

RCB-1.3 TESTING

RCB-1.31 STANDARD TEST The exchanger shall be hydrostatically tested with water. The test pressure shall be held for at least 30 minutes. The shell side and the tube side are to be tested separately in such a manner that leaks at the tube joints can be detected from at least one side. When the tube side design pressure is the higher pressure, the tube bundle shall be tested outside of the shell only if specified by the purchaser and the construction permits. Welded joints are to be



24

sufficiently cleaned prior to testing the exchanger to permit proper inspection during the test. The minimum hydrostatic test pressure at room temperature shall be in accordance with the Code.

RCB-1.311 OTHER LIQUID TESTS Liquids other than water may be used as a testing medium if agreed upon between the purchaser and the manufacturer.

RCB-1.32 PNEUMATIC TEST When liquid cannot be tolerated as a test medium the exchanger may be given a pneumatic test in accordance with the Code. It must be recognized that air or gas is hazardous when used as a pressure testing medium. The pneumatic test pressure at room temperature shall be in accordance with the Code.

RCB-1.33 SUPPLEMENTARY AIR TEST When a supplementary air or gas test is specified by the purchaser, it shall be preceded by the hydrostatic test required by Paragraph RCB-1.31. The test pressure shall be as agreed upon by the purchaser and manufacturer, but shall not exceed that required by Paragraph RCB-1.32.

RCB-1.4 METAL TEMPERATURES

RCB-1.41 METAL TEMPERATURE LIMITATIONS FOR PRESSURE PARTS The metal temperature limitations for various metals are those prescribed by the Code.

RCB-1.42 DESIGN TEMPERATURE OF HEAT EXCHANGER PARTS RCB-1.421 FOR PARTS NOT IN CONTACT WITH BOTH FLUIDS

Design temperatures for the shell and tube sides shall be specified separately by the purchaser. The Code provides the allowable stress limits for parts to be designed at the specified design temperature.

The design temperature is the design metal temperature and is used to establish the Code stress limits for design. The design metal temperature shall be based on the operating temperatures of the shellside and the tubeside fluids, except when the purchaser specifies some other design metal temperature. When the design metal temperature is less than the higher of the design temperatures referred to in Paragraph RCB-1.421, the design metal temperature and the affected parts shall be shown on the manufacturer’s nameplate(s) as described in Paragraph G-3.1.

RCB-1.422 FOR PARTS IN CONTACT WITH BOTH FLUIDS

RCB-1.43 MEAN METAL TEMPERATURES RCB-1.431 FOR PARTS NOT IN CONTACT WITH BOTH FLUIDS

The mean metal temperature is the calculated metal temperature, under specified operating conditions, of a part in contact with a fluid. It is used to establish metal properties under operating conditions. The mean metal temperature is based on the specified operating temperatures of the fluid in contact with the part.

The mean metal temperature is the calculated metal temperature, under specified operating conditions, of a part in contact with both shellside and tubeside fluids. It is used to establish metal properties under operating conditions. The mean metal temperature is based on the specified operating temperatures of the shellside and tubeside fluids. In establishing the mean metal temperatures, due consideration shall be given to such factors as the relative heat transfer coefficients of the two fluids contacting the part and the relative heat transfer area of the parts contacted by the two fluids.

RCB-1.432 FOR PARTS IN CONTACT WITH BOTH FLUIDS

RCB-1.5 STANDARD CORROSION ALLOWANCES The standard corrosion allowances used for the various heat exchanger parts are as follows, un!ess the conditions of service make a different allowance more suitable and such allowance is speclfled by the purchaser.


MECHANICAL STANDARDS TEMA CLASS R C B SECTION 5

RCB-1.51 CARBON STEEL PARTS

R-1.511 PRESSURE PARTS All carbon steel pressure parts, except as noted below, are to have a corrosion allowance of 1 /8" (3.2 mm).

All carbon steel pressure parts, except as noted below, are to have a corrosion allowance of 1/16" (1.6 mm).

Internal floating head covers are to have the corrosion allowance on all wetted surfaces except gasket seating surfaces. Corrosion allowance on the outside of the flanged portion may be included in the recommended minimum edge distance.

CB-1.511 PRESSURE PARTS

RCB-1.512 INTERNAL FLOATING HEAD COVERS

RCB- 1.5 1 3 TUBES HEETS Tubesheets are to have the corrosion allowance on each side with the provision that, on the grooved side of a grooved tubesheet, the depth of the gasketed groove may be considered as available for corrosion allowance.

RCB-1.514 EXTERNAL COVERS Where flat external covers are grooved, the depth of the gasketed groove may be considered as available for corrosion allowance.

RCB-1.515 END FLANGES Corrosion allowance shall be applied only to the inside diameter of flanges where exposed to the fluids.

Nonpressure parts such as tie-rods, spacers, baffles and support plates are not required to have corrosion allowance.

Tubes, bolting and floating head backing devices are not required to have corrosion allowance.

RCB-1.516 NONPRESSURE PARTS

RCB-1.517 TUBES, BOLTING AND FLOATING HEAD BACKING DEVICES

RCB-1.518 PASS PARTITION PLATES Pass partition plates are not required to have corrosion allowance.

RCB-1.52 ALLOY PARTS Alloy parts are not required to have corrosion allowance.

Cast iron pressure parts shall have a corrosion allowance of 1 /8" (3.2 mm).

Cast iron pressure parts shall have a corrosion allowance of 1 /I 6" (1.6 mm).

R-1.53 CAST IRON PARTS

CB-1.53 CAST IRON PARTS

RCB-1.6 SERVICE LIMITATIONS

RB-1.61 CAST IRON PARTS Cast iron shall be used only for water service at pressures not exceeding 150 psi (1034 kPa).

Cast iron shall not be used for pressures exceeding 150 psi (1034 kPa), or for lethal or flammable fluids at any pressure.

C-1.61 CAST IRON PARTS


SECTION 5 MECHANICAL STANDARDS TEMA CLASS R C €3

RCB-1.62 EXTERNAL PACKED JOINTS Packed joints shall not be used when the purchaser specifies that the fluid in contact with the joint is lethal or flammable.

RCB-1.7 ANODES

Selection and placement of anodes is not the responsibility of the heat exchanger manufacturer. If a heat exchanger is to be furnished with anodes, when requesting a quotation, the purchaser is responsible for furnishing the heat exchanger manufacturer the following information: (1) Method of anode attachment. (2) Quantity of anodes required. (3) Size and manufacturer of the anodes. (4) Anode material. (5) Sketch of anode locations and spacing.

If the heat exchanger manufacturer chooses to install anodes for a customer, the manufacturer is not responsible for the suitability of the anodes for the service it is installed in, the life of the anodes, the corrosion protection provided by the anode, or any subsequent damage to the heat exchanger attributed to the anode, the method of anode installation, or the installed location of the anode in the heat exchanger.


MECHANICAL STANDARDS TEMA CLASS R C 6 SECTION 5

O.D. Inches (mm)

Copper and Copper Alloys Carbon Steel, Aluminum Other Alloys and Aluminum Alloys

B.W.G. B.W.G. B.W.G.

114 I (6.4) . .

22

22 20 18 20 18

3/8 (9.5)

1 12 (1 2.7)

27 24

22 22 20 18

20 18

27 24

-~ -

20 18 16

20 18 16 18 16 14 12

1 1 18

5/8

3/4 (19.1)

7/8 (22.2)

(1 5.9) 18 20 16 18 14 16

16 18 14 16 12 14 14 16 12 14 10 12

I 14 I 16 (25.4) 16 12 14

14 12

1-1 14

1-1 /2

2

(31.8)

(38.1 )

(50.8)

Notes: 1. Wall thickness shall be specified as either minimum or average. 2. Characteristics of tubing are shown in Tables D-7 and D7M.

RCB-2.22 INTEGRALLY FINNED TUBES The nominal fin diameter shall not exceed the outside diameter of the unfinned section. Specified wall shall be based on the thickness at the root diameter.

16 14 14 14 12 12 16 14 14 14 12 12 14 14 14 12 12 12



28

RCB-2.3 U-TUBES

RCB-2.31 U-BEND REQUIREMENTS When U-bends are formed, it is normal for the tube wall at the outer radius to thin. The minimum tube wall thickness in the bent portion before bending shall be:

where

t o =

t , =

d o =

R =

Original tube wall thickness, inches (mm) Minimum tube wall thickness calculated by Code rules for a straight tube subjected to the same pressure and metal temperature, inches (mm) Outside tube diameter, inches (mm) Mean radius of bend, inches (mm)

More than one tube gage, or dual gage tubes, may be used in a tube bundle. When U-bends are formed from tube materials which are relatively non-work-hardening and of suitable temper, tube wall thinning in the bends should not exceed a nominal 17% of original tube wall thickness. Flattening at the bend shall not exceed 10% of the nominal tube outside diameter. U-bends formed from tube materials having low ductility, or materials which are susceptible to work-hardening, may require special consideration. Also refer to Paragraph RCB-2.33.

RCB-2.32 BEND SPACING

RCB-2.321 CENTER-TO-CENTER DIMENSION The center-to-center dimensions between parallel legs of U-tubes shall be such that they can be insetted into the baffle assembly without damage to the tubes.

The assembly of bends shall be of workmanlike appearance. Metal-to-metal contact between bends in the same plane shall not be permitted.

RCB-2.322 BEND INTERFERENCE

RCB-2.33 HEAT TREATMENT Cold work in forming U-bends may induce embrittlement or susceptibility to stress corrosion in certain materials and/or environments. Heat treatment to alleviate such conditions may be performed by agreement between manufacturer and purchaser.

RCB-2.4 TUBE PATTERN Standard tube patterns are shown in Figure RCB-2.4.

FIGURE RCB-2.4

30° 60' wo 45O

Triangular Rotated Square Triangular

W

Rotated Square,

Note: Flow arrows are perpendicular to the baffle cut edge.



RCB-2.41 SQUARE PAlTERN In removable bundle units, when mechanical cleaning of the tubes is specified by the purchaser, tube lanes should be continuous.

RCB-2.42 TRIANGULAR PAlTERN Triangular or rotated triangular pattern should not be used when the shell side is to be cleaned mechanically.

R-2.5 TUBE PITCH Tubes shall be spaced with a minimum center-to-center distance of 1.25 times the outside diameter of the tube. When mechanical cleaning of the tubes is specified by the purchaser, minimum cleaning lanes of 1 /4" (6.4 mm) shall be provided.

C-2.5 TUBE PITCH Tubes shall be spaced with a minimum center-to-center distance of 1.25 times the outside diameter of the tube. Where the tube diameters are 5/8" (15.9 mm) or less and tube-to-tubesheet joints are expanded only, the minimum center-to-center distance may be reduced to 1.20 times the outside diameter.

6-23 TUBE PITCH Tubes shall be spaced with a minimum center-to-center distance of 1.25 times the outside diameter of the tube. When mechanical cleaning of the tubes is specified by the purchaser and the nominal shell diameter is 12 inches (305 mm) or less, minimum cleaning lanes of 3/16" (4.8 mm) shall be provided. For shell diameters greater than 12 inches (305 mm), minimum cleaning lanes of 1 /4" (6.4 mm) shall be provided.



Nominal Shell Diameter

6 152) 8-12 1203-305)

(762-991 (330-7371 13 - 29 30 - 39 40 - 60 (1016-1524) 61 -80 (1 549-2032) 81 - 100 (2057-2540)

RCB-3 SHELLS AND SHELL COVERS

RCB-3.1 SHELLS

RCB-3.11 SHELL DIAMETERS

Carbon Steel Pipe Plate

SCH. 40 SCH. 30

SCH. STD 3/8 (9.5) 7/16 1/2 1/2 (12.7) 1/2 (12.7)

It shall be left to the discretion of each manufacturer to establish a system of standard shell diameters within the TEMA Mechanical Standards in order to achieve the economies peculiar to his individual design and manufacturing facilities.


6 (1 52)

24 - 29 (61 0-737) gEE) 8- 12

13 - 23 30 - 39 (762-991) 40 - 60 (1 01 6-1 524) 61 -80 (1 549-2032) 81 - 100 (2057-2540)

RCB-3.12 TOLERANCES

Minimum Thickness Carbon Steel Alloy *

Pipe Plate 118 (3.2)

5/16 (7.9) 3/16 (4.8)

1/2 (12.7) 5/16 (7.9) 1/2 (12.7) 3/8 (9.5)

g:;{ 7/16 3/8 (11.1 (9.5) 1 /4 g::j

SCH. 40 SCH. 30 SCH. 20 5/16 (7.9) 1/8

30

RCB-3.121 PIPE SHELLS The inside diameter of pipe shells shall be in accordance with applicable ASTM/ASME pipe specifications.

RCB-3.122 PLATE SHELLS The inside diameter of any plate shell shall not exceed the design inside diameter by more than 1 /8" (3.2 mm) as determined by circumferential measurement.

RCB-3-13 MINIMUM SHELL THICKNESS Shell thickness is determined by the Code design formulas, plus corrosion allowance, but in no case shall the nominal thickness of shells be less than that shown in the applicable table. The nominal total thickness for clad shells shall be the same as for carbon steel shells.

TABLE R-3.13 MINIMUM SHELL THICKNESS

Dimensions In Inches (mm) Minimum Thickness I

I Alloy *

3/16 (4.8)

5/16 5/16 (7.9) 3/8 (9.5)



RCB-3.2 SHELL COVER THICKNESS Nominal thickness of shell cover heads, before forming, shall be at least equal to the thickness of the shell as shown in the applicable table.

RCB-4 BAFFLES AND SUPPORT PLATES

RCB-4.1 TYPE OF TRANSVERSE BAFFLES The segmental or multi-segmental type of baffle or tube support plate is standard. Other type baffles are permissible. Baffle cut is defined as the segment opening height expressed as a ercentage of the shell inside diameter or as a percentage of the total net free area inside the shell &hell cross sectional area minus total tube area). The number of tube rows that overlap for multi-segmental baffles should be adjusted to give approximately the same net free area flow through each baffle. Baffles shall be cut near the centerline of a row of tubes, of a pass lane, of a tube lane, or outside the tube pattern. Baffles shall have a workmanlike finish on the outside diameter. Typical baffle cuts are illustrated in Figure RCB-4.1. Baffle cuts may be vertical, horizontal or rotated.

FIGURE RCB-4.1 BAFFLE CUTS FOR SEGMENTAL BAFFLES

Horizontal Vertical Rotated

BAFFLE CUTS FOR MULTCSEGMENTAL BAFFLES

DOUBLE SEGMENTAL

TRIPLE SEGMENTAL RCB-4.2 TUBE HOLES

Where the maximum unsupported tube length is 36 inches (914 mm) or less, or for tubes larger in diameter than 1-1 /4 inches (31.8 mm) OD, standard tube holes are to be 1 /32 inch (0.8 mm) over the OD of the tubes. Where the unsupported tube length exceeds 36 inches (91 4 mm) for tubes 1-1 /4 inches (31.8 mm) diameter and smaller, standard tube holes are to be 1 /64 inch (0.4 mm) over the OD of the tubes. For pulsating conditions, tube holes may be smaller than standard. Any burrs shall be removed and the tube holes given a workmanlike finish. Baffle holes will have an over-tolerance of 0.070 inch (0.3 mrn) except that 4% of the holes are allowed an over-tolerance of 0.01 5 inch (0.4 mm).

The transverse baffle and support plate clearance shall be such that the difference bepeen the shell design inside diameter and the outside diameter of the baffle shall not exceed that indicated in Table RCB-4.3. However, where such clearance has no significant effect on shell side heat transfer coefficient or mean temperature difference, these maximurn clearances may be increased to twice the tabulated values. (See Paragraph RCB-4.43.)

RCB-4.3 TRANSVERSE BAFFLE AND SUPPORT CLEARANCE


SECTION 5

Nominal Shell ID 6-17 (1 52-432)

18-39 (457-991) 40 - 54 (1 01 6-1 372

70 - 84 85 - 100

55 ~ 69 (1 397-1 7531

[;;;::;El

MECHANICAL STANDARDS TEMA CLASS R C B

Design ID of Shell Minus Baffle OD 1/8 (3.2)

3/16 1/4 g::]

5/16 (7.9)

7/16 3/8 (11.1 (9*51

TABLE RCB-4.3 Standard Cross Baffle and Support Plate Clearances

Dimensions In Inches (mm)

Nominal Shell ID

6-14 15 - 28 [;"8::%/ 29 - 38 (737-965

61 - 100 (1549-2540 39 - 60

Plate Thickness ~ -~

Unsupportedtube length between central baffles. End spaces between tubesheets and baffles are not a consideration.

24 (610) and Under

Over 24 (61 0) Over 36 (91 4) to 36 (914) to 48 (1219) Inclusive Inclusive

15.9

Over 48 (1219) to 60

(1524) Inclusive

3/4

Over 60 (1 524)

3/8 (9.5 1/2 (12.71 5/8 (15.9)


MECHANICAL STANDARDS TEMA CLASS R c B SECTION 5

Nominal Shell ID

TABLE CB-4.41 BAFFLE OR SUPPORT PLATE THICKNESS

Dimensions in Inches (mm)

Plate Thickness Unsupported tube length between central baffles. End sDaces between

tubesheets and baffle Over 36

(914) to 48 (1219)

Inclusive 114 (6.4) 3/8 (9.5)

(9.5 7;; (12.71 5/8 (15.9)

6 - 14 (1 52-356) 15-28 (381-711) 29 - 38

61 - 100 (1549-2540) 39 - 60 [ ~ ~ ~ ~ ? ! ~ & )

Over 48 Over 60 (1219) to60 (1524)

(1 524) Inclusive

3/8 (9.5) 3/8 (9.5) 3/8 (9.5) 1/2 (12.7) 1/2 12.7 5/8 5/8 l15.91 5/8 [;:::I 314 (19.1) 3/4 (19.1)

12 (305) and Under

1/16 (1.6) 1/8 (3.2) 3/16 4.8 1/4 16.41 114 (6.4)

Over 24 (610) to 36

Inclusive ;I- 3/16 (4.8)

1/2 (12.7)

(91 4)

5/16 [;;;{ 3/8

Over 12 (305) to 24

Inclusive 1/8 (3.2) 3/16 (4.8) 1/4 1/4 [:::I 3/8 (9.5)

(61 0)

R-4.42 LONGITUDINAL BAFFLES Longitudinal baffles shall not be less than 1 /4" (6.4 mm) nominal metal thickness.

CB-4.42 LONGITUDINAL BAFFLES Longitudinal carbon steel baffles shall not be less than 1/4" (6.4 mm) nominal metal thickness. Longitudinal alloy baffles shall not be less than 118" (3.2 mm) nominal metal thickness.

RCB-4.43 SPECIAL PRECAUTIONS Special consideration should be given to: (1) Baffles and support plates subjected to pulsations. (2) Baffles and support plates engaging finned tubes. (3) Longitudinal baffles subjected to large differential pressures due to high shell side fluid

(4) Support of tube bundles when larger clearances allowed by RCB-4.3 are used. pressure drop.

RCB-4.5 SPACING OF BAFFLES AND SUPPORT PLATES

RCB-4.51 MINIMUM SPACING Segmental baffles normally should not be spaced closer than 1 /5 of the shell ID or 2 inches (51 mm), whichever is greater. However, special design considerations may dictate a closer spacing.

Tube support plates shall be so spaced that the unsupported tube span does not exceed the value indicated in Table RCB-4.52 for the tube material used.

RCB-4.52 MAXIMUM SPACING


SECTION 5

Tube OD

1/4 (6.4) 3/8 (9.5)

3/4 (19.1) 7/8 22.2

1 125.4) 1-1/4 (31.8)

34

Carbon Steel & High Alloy Steel, 750

Low Alloy Steel, 850 (454) Nickel-Copper, 600 (31 6) Nickel, 850 (454) Nickel-Chromium-Iron, 1000 (538)

(399)

26 (660) 35 (889)

60 (1524 69

I17531 74 1880 88 (2235)

100 2540 125 I31751


TABLE RCB-4.52 MAXIMUM UNSUPPORTED STRAIGHT TUBE SPANS

Dimensions in Inches (mm)

I Tube Materials and Temperature Limit3 OF (“C)

Aluminum & Aluminum Alloys, Copper & Copper Alloys, Titanium Alloys At Code Maximum Allowable Temperature

30 (762 38 965) 45 11143) 52 (1321)

76 (1930)

110 87 I””I 2794

Notes: (1) Above the metal temperature limits shown, maximum spans shall be reduced in direct

proportion to the fourth root of the ratio of elastic modulus at temperature to elastic modulus at tabulated limit temperature.

(2) In the case of circumferentially finned tubes, the tube OD shall be the diameter at the root of the fins and the corresponding tabulated or interpolated span shall be reduced in direct proportion to the fourth root of the ratio of the weight per unit length of the tube, if stripped of fins to that of the actual finned tube.

induced vibration problems. Refer to Section 6 for vibration criteria. (3) The maximurn unsupported tube spans in Table RCB-4.52 do not consider potential flow

RCB-4.53 BAFFLE SPACING Baffles normally shall be spaced uniformly, spanning the effective tube length. When this is not possible, the baffles nearest the ends of the shell, and or tubesheets, shall be located as

uniformly.

The support plates or baffles adjacent to the bends in U-tube exchangers shall be so located that, for any individual bend, the sum of the bend diameter plus the straight lengths measured along both legs from supports to bend tangents does not exceed the maximum unsupported span determined from Paragraph RCB-4.52. Where bend diameters prevent compliance, special provisions in addition to the above shall be made for support of the bends.

When pulsating conditions are specified by the purchaser, unsupported spans shall be as short as pressure drop restrictions permit. If the span under these circumstances approaches the maximum permitted by Paragraph RCB-4.52, consideration should be given to alternative flow arrangements which would permit shorter spans under the same pressure drop restrictions.

close as practical to the shell nozzles. The remaining ba ft: es normally shall be spaced

RCB-4.54 U-TUBE REAR SUPPORT

RCB-4.55 SPECIAL CASES

RCB-4.56 TUBE BUNDLE VIBRATION Shell side flow may produce excitation forces which result in destructive tube vibrations. Existing predictive correlations are inadequate to insure that any given design will be free of such damage. The vulnerability of an exchanger to flow induced vibration depends on the flow rate, tube and baffle materials, unsupported tube spans, tube field layout, shell diameter, and inlet/outlet configuration. Section 6 of these Standards contains information which is



intended to alert the designer to potential vibration problems. In any case, and consistent with Paragraph G-5, the manufacturer is not responsible or liable for any direct, indirect, or consequential damages resulting from vibration.

RCB-4.6 IMPINGEMENT BAFFLES AND EROSION PROTECTION The following paragraphs provide limitations to prevent or minimize erosion of tube bundle components at the entrance and exit areas. These limitations have no correlation to tube vibration and the designer should refer to Section 6 for information regarding this phenomenon.

RCB-4.61 SHELL SIDE IMPINGEMENT PROTECTION REQUIREMENTS An impingement plate, or other means to protect the tube bundle against impinging fluids, shall be provided when entrance line values of p V * exceed the following: non-abrasive, single phase fluids, 1500 (2232); all other liquids, including a liquid at its boiling point, 500 (744). For all other gases and vapors, including all nominally saturated vapors, and for liquid vapor mixtures, impingement protection is required. I/ is the linear velocity of the fluid in feet per second (meters per second) and p is its density in pounds per cubic foot (kilograms per cubic meter). A properly designed diffuser may be used to reduce line velocities at shell entrance.

*RCB-4.62 SHELL OR BUNDLE ENTRANCE AND EXIT AREAS

In no case shall the shell or bundle entrance or exit area produce a value of p I/ in excess of 4,000 (5953) where V is the linear velocity of the fluid in feet per second (meters per second) and p is its density in pounds per cubic foot (kilograms per cubic meter).

*RCB-4.621 SHELL ENTRANCE OR EXIT AREA WITH IMPINGEMENT PLATE When an impingement plate is provided, the flow area shall be considered the unrestricted area between the inside diameter of the shell at the nozzle and the face of the impingement plate.

*RCB-4.622 SHELL ENTRANCE OR EXIT AREA WITHOUT IMPINGEMENT PLATE For determining the area available for flow at the entrance or exit of the shell where there is no impingement plate, the flow area between the tubes within the projection of the nozzle bore and the actual unrestricted radial flow area from under the nozzle or dome measured between the tube bundle and shell inside diameter may be considered.

*RCB-4.623 BUNDLE ENTRANCE OR EXIT AREA WITH IMPINGEMENT PLATE When an impingement plate is provided under a nozzle, the flow area shall be the unrestricted area between the tubes within the compartments between baffles and/or tubesheet.

"RCB-4.624 BUNDLE ENTRANCE OR EXIT AREA WITHOUT IMPINGEMENT PLATE For determining the area available for flow at the entrance or exit of the tube bundle where there is no impingement plate, the flow area between the tubes within the compartments between baffles and/or tubesheet may be considered.

RCB-4.63 TUBE SIDE Consideration shall be given to the need for special devices to prevent erosion of the tube ends under the following conditions: (1) Use of an axial inlet nozzle. (2) Liquid p V is in excess of 6000 (8928)' where I/ is the linear velocity in feet per second

(meter per second), and p is its density in pounds per cubic foot (kilograms per cubic meter).

RCB-4.7 TIE RODS AND SPACERS Tie rods and spacers, or other equivalent means of tying the baffle system together, shall be provided to retain all transverse baffles and tube support plates securely in position.




Minimum

Rods

Tie Rod Diameter Number of Tie

6-15 16-27 28 - 33 (71 1-838) 34 - 48 49 - 60

(864-1 2 1 9 (1 245-1 5241

61 -1 00 (1 549-2540)


6 - 15 (7 52-381) 16 - 27 (406-686) 28 - 33 34 - 48 49 - 60 61-100

&:::%)

1/2 (12.7)

5/8 (15.9)

Tie R o d Minimum Diameter Number of Tie

Rods

1/4 (6.4) 4 318 (9.5) 6

6 1/2 1'"3 12.7 8

10 12 5/8 (15.9

4 6 6 0 10 12

RCB-4.8 SEALING DEVICES In addition to the baffles, sealing devices should be installed when necessary to prevent excessive- fluid by-passing around or through the tube bundle. Sealing devices may be seal strips, tle rods with spacers, dummy tubes, or combinations of these.

For kettle type reboilers, skid bars and a bundle holddown may be provided. One method is shown in Figure RCB-4.9. Other methods which satisfy the intent are acceptable. Bundle hold-downs are not required for fixed tubesheet kettles.

RCB-4.9 KElTLE TYPE REBOILERS



FIGURE RCB-4.9

SECTION 5

CROSS-SECTION END VIEW OF TUBE BUNDLE AND SHELL



RCB-5 FLOATING END CONSTRUCTION

RCB-5.1 INTERNAL FLOATING HEADS (Types S and T)

R-5.11 MINIMUM INSIDE DEPTH OF FLOATING HEAD COVERS For multipass floating head covers the inside depth shall be such that the minimum cross-over area for flow between successive tube passes is at least equal to 1.3 times the flow area through the tubes of one pass. For single pass floating head covers the depth at nozzle centerline shall be a minimum of one-third the inside diameter of the nozzle.

CB-5.11 MINIMUM INSIDE DEPTH OF FLOATING HEAD COVERS For multipass floating head covers the inside depth shall be such that the minimum cross-over area for flow between successive tube passes is at least equal to the flow area through the tubes of one pass. For single pass floating head covers the depth at nozzle centerline shall be a minimum of one-third the inside diameter of the nozzle.

RCB-5.12 POSTWELD HEAT TREATMENT Fabricated floating head covers shall be postweld heat treated when required by the Code or specified by the purchaser.

RCB-5.13 INTERNAL BOLTING The materials of construction for internal bolting for floating heads shall be suitable for the mechanical design and similar in corrosion resistance to the materials used for the shell interior.

RCB-5.14 FLOATING HEAD BACKING DEVICES The material of construction for split rings or other internal floating head backing devices shall be equivalent in corrosion resistance to the material used for the shell interior.

RCB-5.141 BACKING DEVICE THICKNESS (TYPE S) The required thickness of floating head backing devices shall be determined by the following formulas or minimum thickness shown in Figure RCB-5.141, using whichever thickness is greatest. BENDING

SHEAR

W

A =

B =

C =

N =

Ring OD, inches (mm) W =

As shown in Fig. Y = RCB-5.141, inches (mm) Bolt circle, inches (mm)

( k - B ) / 2 , inches (mrn)

z =

L =

where

Design bolt load (as ref. in Code Appendix 2), Ib. (kN) From Code Fig. 2-7.1 using K = A / B

Tubesheet OD, inches (rnm)

Greater of T o r t , inches (mm)



S = Code allowable stress in tension (using shell design temperature), psi (kPa)

S t)r = S of backing ring, psi (kPa) S k r = S of split key ring, psi (kPa) S,, = S of tubesheet, psi (kPa)

s, = 0.8s , psi (kPa)

NOTES 1. All references above are to ASME Code Section VIII, Division 1.

2. Caution: For styles "A , "B" & "D" check thickness in shear of the tubesheet if

3. Caution: Style " C check thickness in shear of the tubesheet if S Ls < S f r

s,, < S b ,

See Figure RCB-5.141 for illustration of suggested styles. Other styles are permissible. FIGURE RCB 5.141

ANGLE=4S (0.8 RAD) MIN, 75' (1.3 RAD) MAX

STYLE "A"

SPLIT KEY RING

t t 1/64"(0.4)

STYLE "C"

SPLIT RlNG,t~i I-. OPTIONAL

STYLE "B"

1 /32"(0.8) I I - tMAXl

STYLE "D"

~



40

RCB-5.15 TUBE BUNDLE SUPPORTS When a removable shell cover is utilized, a partial support plate, or other suitable means, shall be provided to support the floating head end of the tube bundle. If a plate is used, the thickness shall equal or exceed the support plate thickness specified in Table R-4.41 or CB-4.41 as applicable for unsupported tube lengths over 60 inches (1524 mm).

RCB-5.16 FLOATING HEAD NOZZLES The floating head nozzle and packing box for a single pass exchanger shall comply with the requirements of Paragraphs RCB-5.21, RCB-5.22 and RCB-5.23.

RCB-5.17 PASS PARTITION PLATES The nominal thickness of floating head pass partitions shall be identical to those shown in RCB-9.13 for channels and bonnets.

RCB-5.2 OUTSIDE PACKED FLOATING HEADS (Type P)

RCB-5.21 PACKED FLOATING HEADS The cylindrical surface of packed floating head tubesheets and skirts, where in contact with packing (including allowance for expansion), shall be given a fine machine finish equivalent to 63 microinches.

RCB-5.22 PACKING BOXES A machine finish shall be used on the shell or packing box where the floating tubesheet or nozzle passes through. If packing of braided material is used, a minimum of three rings of packing shall be used for 150 PSI (1034 kPa) maximum design pressure and a minimum of four rings shall be used for 300 PSI (2068 kPa) maximum design pressure. For pressures less than 150 PSI (1034 kPa), temperatures below 300" F (149" C), and non-hazardous service, fewer rings of packing may be used. Figure RCB-5.22 and Table RCB-5.22 show typical details and dimensions of packing boxes.

Standards Of The Tu~iacZxchanger-~.Nlanufacturers Association


C

1-114 1-114 1-114 1-114 1-114 13/4 1-314 1-314 2-118 2-118

PACKING

D E F BOLTS WIN) NO. SIZE

4 518 6 518 8 518 10 518 12 518

2-114 1-118 1 20 518 2-114 1-118 1 24 518 2-314 1-114 1-114 28 518

1-518 1 3/4 1-518 1 314 1-518 1 314 1-518 1 314

16 5/8 1-5/8 1 314 2-1/4 1-1/8 1

2-314 1-114 1-1/4 32 518

FIGURE RCB-5.22

E

WIN) 25.40 25.40 25.40 25.40 25.40 28.58 28.58 28.58 31.75 31.75

c E

F BOLTS

NO. SIZE 19.05 4 M16 19.05 6 M16 19.05 8 M16 19.05 10 M16 19.05 12 M16 25.40 16 M16 25.40 20 M16 25.40 24 M16 31.75 28 M16 31.75 32 M16

Design Based On SquoreJ \-Packing of Other Suitable Braided Packing Materials. Dimensions, and

Shape May Be Used TABLE RCB-5.22

TYPICAL DIMENSIONS FOR PACKED FLOATING HEADS

150 PSl(1034 kPa) AND 300 PSl(2068 kPa) WITH 600 * F (316 O C) MAX. TEMP

SIZE 152-203 229-330 356-432 457-533 559-584 61 0-737 762-838 864-1 092

1118-1295 1321 -1 524

6 - 8 9 - 13

14 - 17 18 - 21 22 - 23 24 - 29 30 - 33 34 - 43 44 - 51 52 - 60

9.53 11.11 31.75 41.28 9.53 11.11 31.75 41.28 9.53 11.11 31.75 41.28 9.53 11.11 31.75 41.28 9.53 11.11 31.75 41.28

12.70 14.29 44.45 57.15 12.70 14.29 44.45 57.15 12.70 14.29 44.45 57.15 15.88 17.46 53.98 69.85 15.88 17.46 53.98 69.85

B

711 6 711 6 7/16 711 6 711 6 9/16 911 6 911 6 11/16 11/16

Dimensions in Millimeters



Nominal Shell Inside Diameter Inches (mm)

RCB-5.23 PACKING MATERIAL Purchaser shall specify packing material which is compatible with the shell side process conditions.

RCB-5.24 FLOATING TUBESHEET SKIRT The floating tubesheet skirt normally shall extend outward. When the skirt must extend inward, a suitable method shall be used to prevent stagnant areas between the shell side nozzle and the tubesheet.

RCB-5.25 PASS PARTITION PLATES The nominal thickness of floating head pass partitions shall be identical to those shown in Paragraph RCB-9.13 for channels and bonnets.

RCB-5.3 EXTERNALLY SEALED FLOATING TUBESHEET (Type W)

Maximum Design Pressure PSI (kPa)

RB-5.31 LANTERN RING The externally sealed floating tubesheet using square braided packing materials shall be used only for water, steam, air, lubricating oil, or similar services. Design temperature shall not exceed 375 O F (191 O C) . Design pressure shall be limited according to Table RB-5.31.

6 - 24 (152-610) 25 - 42 (635-10671 43 - 60 61 - 100 (1 549-2540)

(1 092-1 524

300 (2068) 150 1034) 75 [517) 50 (345)

C-5.31 LANTERN RING The externally sealed floating tubesheet shall be used only for water, steam, air, lubricating oil, or similar services. Design temperature, pressure and shell diameter shall be limited by the service, joint configuration, packing material and number of packing rings, to a maximum design pressure of 600 psi (4137 kPa).

The design shall incorporate provisions in the lantern ring so that any leakage past the packing will leak to atmosphere. When endless packing rings are used, one ring of packing shall be used on each side of the lantern ring. For braided packing materials with a seam, a minimum of two rings of packing shall be used on each side of the lantern ring, with the seams staggered during assembly.

RCB-5.32 LEAKAGE PRECAUTIONS

RCB-5.33 PACKING MATERIAL Purchaser shall specify packing material which is compatible with the process conditions.

RCB-5.34 SPECIAL DESIGNS Special designs incorporating other sealing devices may be used for the applications in Paragraph RB-5.31 and C-5.31 or other special service requirements. Provisions for leak detection shall be considered.

42 Standards Of The Tubular-Exchanger- Manufacturers Association


RCB-6 GASKETS

RCB-6.1 TYPE OF GASKETS Gaskets shall be selected which have a continuous DeriDherv with no radial leak paths. This shall not exclude gaskets made continuous by welding or other methbds which produce a homogeneous bond.

R-6.2 GASKET MATERIALS Metal jacketed or solid metal gaskets shall be used for internal floating head joints, all joints for pressures of 300 psi (2068 kPa) and over, and for all joints in contact with hydrocarbons. Other gasket materials may be specified by agreement between purchaser and manufacturer to meet special service conditions and flange design. When two gasketed joints are compressed by the same bolting, provisions shall be made so that both gaskets seal, but neither gasket is crushed at the required bolt load.

CB-6.2 GASKET MATERIALS For design pressures of 300 psi (2068 kPa) and lower, composition gaskets may be used for external joints, unless temperature or corrosive nature of contained fluid indicates otherwise. Metal jacketed, filled or solid metal gaskets shall be used for all joints for design pressures greater than 300 psi (2068 kPa) and for internal floating head joints. Other gasket materials may be specified by agreement between purchaser and manufacturer to meet special service conditions and flange design. When two gasketed joints are compressed by the Same bolting, provisions shall be made so that both gaskets seal, but neither gasket is crushed at the required bolt load.

RCB-6.3 PERIPHERAL GASKETS RC-6.31

The minimum width of peripheral ring gaskets for external joints shall be 3/8" (9.5 mm) for shell sizes through 23 inches (584 mm) nominal diameter and 1 /2" (1 2.7 mm) for all larger shell sizes.

The minimum width of peripheral ring askets for external joints shall be 3/8" (9.5 mm) for shell sizes through 23 inches (584 mmy nominal diameter and 1 /2" (1 2.7 mm) for all larger shell sizes. Full face gaskets shall be used for all cast iron flanges.

The minimum width of peripheral ring gaskets for internal joints shall be 1 /4" (6.4 mm) for all shell sizes.

Peripheral gasket contact surfaces shall have a flatness tolerance of * 1 /32" (0.8 mm) maximum deviation from any reference plane. This maximum deviation shall not occur in less than a 20 O (0.3 Rad) arc.

Flatness of peripheral gasket contact surfaces shall be sufficient to meet the requirements of Paragraph RCB-1.3.

8-6.31

RCB-6.32

R-6.33

CB-6.33

RCB-6.4 PASS PARTITION GASKETS The width of gasket web for pass partitions of channels, bonnets, and floating heads shall be not less than 1 /4" (6.4 mm) for shell sizes through 23 inches (584 mm) nominal diameter and not less than 3 / 8 (9.5 mm) for all larger shell sizes.

Gasketed joints shall be of a confined type. R-6.5 GASKET JOINT DETAILS



CB-6.5 GASKET JOINT DETAILS Gasket joints shall be of a confined or unconfined type.

FIGURE RCB-6.5

-----

Confined Gasket Unconfined Gasket

For dimensions and tolerances, see Figure F-3.

44

Confined Gasket

SPIRAL WOUND GASKET WITH OUTER METAL RING

RCB-6.6 SPARE GASKETS Unless specifically stated otherwise, spare gaskets include only main body flange gaskets.



RCB-7 TUBESHEETS

RCB-7.1 TUBESHEET THICKNESS

RCB-7.11 APPLICATION INSTRUCTIONS AND LIMITATIONS Subject to the requirements of the Code, the formulas and design criteria contained in Paragraphs RCB-7.1 through RCB-7.25 are applicable, with limitations noted, when the following normal design conditions are met: (1) Size and pressure are within the scope of the TEMA Mechanical Standards, Paragraph

RCB-1.1

(2) Tube-to-tubesheet joints are expanded, welded or otherwise constructed such as to effectively contribute to the support of the tubesheets (except U-tube tubesheets)

(3) Tubes are uniformly distributed (no large untubed areas) Abnormal conditions of support or loading are considered Special Cases, and are defined in Paragraph RCB-7.3 which is referenced, when pertinent, in subsequent paragraphs.

RCB-7.12 EFFECTIVE TUBESHEET THICKNESS Except as qualified by Paragraphs RCB-7.121 and 7.122, the effective tubesheet thickness shall be the thickness measured at the bottom of the tube side pass partition groove and/or shell side longitudinal baffle groove minus corrosion allowance in excess of the groove depths.

RCB-7.121 APPLIED TUBESHEET FACINGS The thickness of applied facing material shall not be included in the minimum or effective tubesheet thickness.

RCB-7.122 INTEGRALLY CLAD TUBESHEETS The thickness of cladding material in integrally clad plates and cladding deposited by welding may be included in the effective tubesheet thickness as allowed by the Code.

RCB-7.13 REQUIRED EFFECTIVE TUBESHEET THICKNESS The required effective tubesheet thickness for any type of heat exchanger shall be determined from the following paragraphs, for both tube side and shell side conditions, corroded or uncorroded, using whichever thickness is greatest. Both tubesheets of fixed tubesheet exchangers shall have the same thickness, unless the provisions of Paragraph RCB-7.166 are satisfied.

R-7.131 MINIMUM TUBESHEET THICKNESS WITH EXPANDED TUBE JOINTS In no case shall the total thickness minus corrosion allowance, in the areas into which tubes are to be expanded, of any tubesheet be less than the outside diameter of tubes. In no case shall the total tubesheet thickness, including corrosion allowance, be less than 3/4" (19.1 mm).

In no case shall the total thickness minus corrosion allowance, in the areas into which tubes are to be expanded, of any tubesheet be less than three-fourths of the tube outside diameter for tubes of 1" (25.4 mm) OD and smaller, 7/8" (22.2 mm) for 1-1 /4" (31.8 mm) OD, 1" (25.4 mm) for 1-1 /2" (38.1 mm) OD, or 1-1 /4" (31.8 mm) for 2" (50.8 mm) OD.

In no case shall the total thickness minus corrosion allowance, in the areas into which tubes are to be expanded, of any tubesheet be less than three-fourths of the tube outside diameter for tubes of 1" (25.4 mm) OD and smaller, 7/8 (22.2 mm) for 1-1 /4" 31.8 mm) OD, 1" (25.4) for 1-1 /2" (38.1 mm) OD, or 1-1 /4" (31.8 mm) for 2" (50.8 mm) b D. In no case shall the total tubesheet thickness, including corrosion allowance, be less than 3/4" (19.1 mm).

C-7.131 MINIMUM TUBESHEET THICKNESS WITH EXPANDED TUBE JOINTS

8-7.131 MINIMUM TUBESHEET THICKNESS WITH EXPANDED TUBE JOINTS


SECTION 5

G shall be either in the corroded or uncorroded condition, dependent upon which condition is under consideration. For fixed tubesheet exchangers, G shall be the shell inside diameter. For kettle type exchangers, G shall be the port inside diameter. For any floating tubesheet (except divided), G shall be the G used for the stationary tubesheet using the Pas defined for other type exchangers. Type T tubesheets shall also be checked using the pressure P defined above with bolting and using the actual gasket G of the floating tubesheet For a divided floating tubesheet, G shall be 1.41 (d) where d is the length of the shortest span measured over centerlines of gaskets. For other type exchangers, G shall be the diameter, inches (mm), over which the pressure under consideration is acting. (e.g.: Pressure acting on the gasketed

1 side of a tubesheet, G = the diameter at the location of the gasket load reaction as defined in the Code. Pressure acting on an integral side of a tubesheet, G = the inside diameter of the integral pressure part.)

46


RCB-7.132 TUBESHEET FORMULA - BENDING

where T = Effective tubesheet thickness, inches (mm). S = Code allowable stress in tension, psi (kPa), for tubesheet material at design

metal temperatures. (See Paragraph RCB-1.42).

P =

G =

:or outside packed floating head exchangers (Type P), Pshall be as defined in 'aragraph RCB-7.141, psi (kPa). -or packed floating end exchangers with lantern ring (Type W), for the floating ubesheet, Pshall be as defined in Paragraph RCB-7.142, psi (kPa). :or fixed tubesheet exchangers, P shall be as defined in Paragraph 3CB-7.163, RCB-7.164 or RCB-7.165, psi (kPa). :or other type exchangers, P shall be the design pressure, shell side or tube ;ide, corrected for vacuum when present on the opposite side, or differential Jressure when specified by the purchaser, psi (kPa). -or U-tube tubesheets (Type U), where the tubesheet is extended as a flange for Jolting to heads or shells with ring type gaskets, P = P + P or P + P b

jepending upon the side under consideration.

where -6.2 M * F 2 G 3

P , =

and A4 *is defined in Paragraph RCB-7.1342, psi (kPa).

For floating tubesheets (Type T), where the tubesheet is extended for bolting to heads with ring type gaskets, the effect of the moment acting upon the extension is defined in Paragraph RCB-7.162 in terms of equivalent tube side and shell side bolting pressures except G shall be the gasket G of the floating tubesheet. P psi (kPa) is given by the greatest absolute value of the following:

P = P , + P B 1

orP=P,-P,, orP = P , o r P = P,

StandardsOf The Tu biilar Excianger-Manufacture= Association


r l =

0.785 1 - for square or rotated square tube patterns (-I2 I 1 - 0iiz,”7,2 for triangular or rotated triangular tube patterns

\ z i z z j - I For integrally finned tubes, the OD of the tube in the tubesheet shall be used.

F =

:or unsupported tubesheets (e.g.: U-tube tubesheets) gasketed both ides, F = 1.25. :or supported tubesheets (e. .: fixed tubesheets and floating type ubesheets) gasketed both sdes, F = 1 .O. :or unsup orted tubesheets (e.g.: U-tube. tubesheets) integra! with either

:igure RCB-7.132. ’or supported tubesheets . e.g.: fixed tubesheets and floating type

letermined by the curve H in Figure RCB-7.132.

)r both si C P es, F shall be the value determined by the curve U in

ubesheets) integral with el I: her or both sides, F shall be the value

FIGURE RCB-7.132 1.30 1.25 1.20 1.15 1.10 1.05 1-00 0.95 0.90 0.85 0.80 0.75 I

0.00 0.01 0.02 0.03 0.04 0.05 0.06 0.07 0.08 0.09 0.10

Wall Thickness/lD Ratio For Integral Tubesheets

NOTE: If the tubesheet is integral with both the tube side and shell side, Wall Thickness and ID are to be based on the side yielding the smaller value of F.

See Table RCB-7.132 for illustration of the application of the above equations.



TABLE RCB - 7.132

TUBESHEET THICKNESS FOR BENDING Note: Must be calculated for shell side or

tube side pressure, whichever is controllina.

S = Code allowable stress in or n Q Tube pattern

a = - [ 3 1 1 tension, psi (kPa), for Tube O D pattern TYDe O D tubesheet material at

the OD of the tube in the

.-. f-

1 .o

1.25

See Figure RCB7.132 [ 17- loo(;)]

15 F = ~

Note: F Max = 1.0 F Min = 0.8

-

Table RCB - 7.1 32 continued next page

G ;hell Side 'ressure

jasket G ;hell side

See note 1

SasketG ,

;hell side

See note 1

Gasket G shell side

See note 1

Shell ID or port inside diameter for kettle type exchangers

Shell ID or port inside diameter for kettle type exchangers

rube Side 'ressure

3asket G tube side

See note 1

Basket G tube side

See note 1

Channel ID

Gasket G (shell ID if fixed tubesheet type unit)

See note 1

Channel ID (shell ID if fixed tubesheet type unit)

P

Design pressure, psi (kPa), shell side or tube side, per Paragraph RCB7.132 corrected for vacuum when Dresent on opposite side or differential pressure when specified by customer.

Design pressure, psi (kPa), shell side or tube side, per Paragraph RCB-7.132 corrected for vacuum when present on opposite side or differential pressure when specified by customer.

Design pressure, psi (kPa), sheli side or tube side, per RCB-7.132 corrected for vacuum when present on opposite side or differential pressure when specified by customer, or fixed tubesheet type units, as defined in Paragraphs RCB-7.163 thru RCB-7.165



Shell Side 'ressure

SECTION 5

2asket G ;hell side

See note t

1 - 7.132 (Continued) G

Shell ID or port nside diameter lor kettle type gxchangers

TABLE R( P F

rube Side Jressure -

ksign pressure, psi (kPa), hell side, ortube side, per Jaragraph RCB-7.132 :orrected for vacuum when )resent on opposite side, or lifferential pressure when ,pecified by customer.

Shannel ID See Figure RC57.132 [ 17 - loo( k)]

12 F =

Note: F Max = 1.25 FMin = 1.00

Gasket G tube side

See note 1

iell. ID or port side diameter lr kettle type (changers

Channel ID

)esign pressure, psi (kPa), shell side, or tube side, per Jaragraph RCE7.132 :orrected for vacuum when >resent on opposite side, or jifferential pressure when ;pecified by customer.

1 .o Same G as used for stationary

tubesheet

Same G as used for stationary ubesheet. Also check using gaske

G of the floating tubesheet See note 1

See Paragraph RCE7.132 1 .o

;= 1.41(d) 1 - Shortest span measured over

center lines of gaskets.

Design pressure, psi (kPa), shell side, or tube side, per Paragraph RCB-7.132 corrected for vacuum when present on opposite side, 01 differential pressure when specified by customer. i Design pressure, psi (kPa), tube side per paragraph RCE7.132 corrected for vacuum when present on the shell side.

Same G as used for stationary tubesheet

Same G as used for stationary tubesheet

Defined in Paragraph RCB-7.1411

Notes: 1 .Gasket G =the diameter at the location of the gasket load reaction as defined in the Code.


SECTION 5

P =

50

For outside packed floating head exchangers (Type P), Pshall be as defined in Paragraph RCB-7.141, psi (kPa).

For fixed tubesheet exchangers, Pshall be as defined in Paragraphs RCB-7.163, RCB-7.164 or RCB-7.165, psi (kPa).

For other type exchangers, Pshall be the design pressure, psi (kPa), shell side or tube side, corrected for vacuum when present on the opposite side, or differential pressure when specified by the purchaser.


RCB-7.133 TUBESHEET FORMULA - SHEAR

where . T = Effective tubesheet thickness, inches (mm)

4 A Equivalent diameter of the tube center limit perimeter, inches D L = - = (mm)

C = Perimeter of the tube layout measured stepwise in increments of one tube pitch from center-to-center of the outermost tubes, inches (mm). Figure RCB-7.133 shows the application to typical triangular and square tube patterns

FIGURE RCB-7.133

'I C" (perimeter) is the length of the heavy line

A = Total area enclosed by perimeter C, square inches (mm 2)

d o = Outside tube diameter, inches (mm), for integrally finned tubes, the OD of the tube in the tubesheet shall be used.

Pi tch = Tube center-to-center spacing, inches (mm)

s = Code allowable stress in tension, psi (kPa), for tubesheet material at design metal temperature. (See Paragraph RCB-1.42.)

NOTE: Shear will not control when

See Table RCB-7.133 for illustration of the application of the above equations.



d o =Outside tube diameter, inches (mm). For integrally finned tubes, the OD of the tube in the tubesheet shall be

TABLE RCB-7.133

Pi tch = Tube spacing, center-toeenter, inches (mm).

TUBESHEET THICKNESS FOR SHEAR 0.31 D Note: Must be calculated for shell side or

tube side pressure, whichever is controlling.

P Design pressure, psi (kPa), shell side or tube side, corrected for vacuum when present on opposite side, or differential pressure when specified by customer

Design pressure, psi (kPa), shell side or tube side, corrected for vacuum when present on opposite side, or differential pressure when specified by customer

Design pressure, psi (kPa), shell side or tube side, corrected for vacuum when present on opposite side, or differential pressure when specified by customer, or for fixed tubesheet type units, as defined in paragraphs RCB-7.163 thru RCB-7.165

TABLE RCB-7.133 Continued next page

3 =Code allowable stress in tension, psi (kPa). For tubesheet material at design metal temperature.(See paragraph RCB-1.42.)

D,

Perimeter of tube layout measured stepwise in increments of one tube-to-tube pitch center-to-center of the outermost tubes, in inches (mm). See Figure RCB7.133

total area enclosed by C in square inches (mm 2). See Figure RCB-7.133



TABLE RCB-7.133 Continued

P lesign pressure, psi (kPa), shell side or tube ;ide, corrected for vacuum when present on ipposite side, or differential pressure when pecified by customer

besign pressure, psi (kPa). Shell side or tube ide, corrected for vacuum when present on lpposite side, or differential pressure when pecified by customer

lesign pressure, psi (kPa), shell side or tube side, corrected for vacuum when present on Ipposite side, or differential pressure when ;pecified by customer

Design pressure, psi (kPa), tube side, corrected for vacuum when present on the shell side

Defined in Paragraph RCB-7.1412

Perimeter of tube layout measured stepwise in increments of one tube-to-tube pitch center-to-center of the outermost tubes, in inches (mm). See Figure

total area enclosed by C in square inches (mm2). See Figure RCB-7.133

RCB-7.133



RCB-7.134 TUBESHEET FORMULA - TUBESHEET FLANGED EXTENSION This paragraph is applicable only when bolt loads are transmitted, at the bolt circle, to the extended portion of a tubesheet. The peripheral portion extended to form a flange for bolting to heads or shells with ring type gaskets may differ in thickness from that portion inside the shell calculated in Paragraph RCB-7.132. The minimum thickness of the extended portion may be calculated from the following paragraphs.

RCB-7.1341 FIXED TUBESHEET OR FLOATING TUBESHEET EXCHANGERS

S ( A - G ) ( 1 + 1 . 8 6 l n r 2 ) r ) 1 1 ‘ 2 M ( r 2 - 1 + 3 . 7 1 r 2 T , = 0.98

where I, = Minimum thickness of the extended portion, inches (mm)

A = Outside diameter of the tubesheet, inches (mm)

A r = G -

M = the larger of A4 I or h4, as defined in Paragraph RCB-7.162

Note: The moments may differ from the moments acting on the attached flange. S and G are defined in Paragraph RCB-7.132

RCB-7.1342 U-TUBE TUBESHEET EXCHANGERS

w11’2 M * + M + 0 . 3 9 P G 2 T , = 1 ,38[

( A - G ) s where

T = Minimum thickness of the extended portion, inches (mm) 3

E w F 3 P G 3 ( : ) rl - M G - 0 . 3 9 w P G 3 M* = G+”(>) 3 w

rl

T = Effective tubesheet thickness calculated from Paragraph RCB-7.132, inches (rnm)

( A - G I 2 W =

M = the larger of M or M as defined in Paragraph RCB-7.162

Note: The moments may differ from the moments acting on the attached flange. F , G and q are defined in Paragraph RCB-7.132

P = P or P or maximum differential pressure, as applicable.

Note: See Paragraph RCB-7.13421 for procedure.


SECTION 5

54


RC57.13421 ITERATIVE CALCULATION METHODS

Method 1

(1) Calculate M * assuming T = T.

(2) Calculate P b then P from Paragraph RCB-7.132.

(3) Calculate T from Paragraph RCB-7.132.


(5) Compare T and T ,.; if 7- is greater than T ,., calculation is terminated. Use T calculated. Do not proceed to Step (6).

(6) If T is greater than T, or if it is desired to reduce T below T, select a new ratio of T / T that is less than 1 and repeat Steps (1) through (5). (Note: T 1 T ratio is calculated using actual corroded thickness of the part).

Method 2 - (ALTERNATIVE METHOD)

(1) SetM* = -A4

(2) Calculate P b then P from Paragraph RCB-7.132.

(3) Calculate Tfrom Paragraph RCB-7.132.


(5) Recalculate M * = - A4 using values of T and T obtained in Steps (3) and (4) and as defined in Paragraph RCB-7.1342. (Note T / T must be 5 1).

(6) If I M * I obtained in Step (5) is less than 1 M lfrom Step (l), calculation is terminated. Use T ,. calculated in Step (4). Do not proceed to Step (7).

(7) If I M * I obtained from Step (5) is greater than 1 A4 1 from Step (l), repeat Step (2) using M * calculated in Step (5). Then repeat Steps (3) through (5).

(8) If last calculated I M * I is less than the previous I M * I used to calculate P b,

calculation is terminated. Use last calculated value of T r .

(9) If last calculated I M * I is greater than the previous I M * I used to calculate P b , repeat Step (2) using last calculated M * Then repeat Steps (3) through (5). Continue this process until Step (8) is satisfied.



RCB-7.14 PACKED FLOATING TUBESHEET TYPE EXCHANGERS EFFECTIVE PRESSURE

RCB-7.141 OUTSIDE PACKED FLOATING HEAD (TYPE P) The thickness of tubesheets in exchangers whose floating heads are packed at the outsidediameter of the tubesheet or a cylindrical extension thereof shall be calculated like stationary tubesheets using the formulas for Pas defined below.

RCB-7.1411 EFFECTIVE DESIGN PRESSURE - BENDING The effective design pressure to be used with the formula shown in Paragraph RCB-7.132 is given by:

1 1 . 2 5 ( D 2 - D , 2 ) ( D - D , ) D F ~ G ~

P = P I + P ,

where P , =

P , =

D =

Design pressure, psi (kPa), tube side (For vacuum design, P , is negative.)

Design pressure, psi (kPa), shell side (For vacuum design, P is negative.)

Outside diameter of the floating tubesheet, inches (mm)

D = J 4A Equivalent diameter of the tube center limit perimeter, inches

F and G are as defined in Paragraph RCB-7.132

(mm), using A as defined in Paragraph RCB-7.133

RCB-7.1412 EFFECTIVE DESIGN PRESSURE - SHEAR The effective design pressure to be used with the formula shown in Paragraph RCB-7.133 is given by:

using terms as defined in Paragraph RCB-7.1411,

RCB-7.142 PACKED FLOATING TUBESHEET WITH LANTERN RING (TYPE W) The thickness of floating tubesheets in exchangers whose floating tubesheets are packed at the outside diameter with return bonnet or channel bolted to the shell flange, shall be calculated as for gasketed stationary tubesheet exchangers, using P defined as the tube side design pressure, psi (kPa), corrected for vacuum when present on the shell side. It is incorrect to utilize the shell side pressure.

RCB-7.15 DOUBLE TUBESHEETS Double tubesheets may be used where the operating conditions indicate their desirability. The diversity of construction types makes it impractical to specify design rules for all cases. Paragraphs RCB-7.154, RCB-7.155 and RCB-7.156 provide the design rules for determining the thickness of double tubesheets for some of the most commonly used construction types.

Neither component of a double tubesheet shall have a thickness less than that required by Paragraph RCB-7.131.

RCB-7.151 MINIMUM THICKNESS


SECTION 5

56

MECHANICAL STANDARDS TEMA CLASS R C 6

RC57.152 VENTS AND DRAINS Double tubesheets of the edge welded type shall be provided with vent and drain connections at the high and low points of the enclosed space.

When double tubesheets are used, special attention shall be given to the ability of the tubes to withstand, without damage, the mechanical and thermal loads imposed on them by the construction.

The tubesheets are connected in a manner which distributes axial load and radial thermal expansion loads between tubesheets by means of an interconnecting element capable of preventing individual radial growth of tubesheets. It is assumed that the element is rigid enough to mutually transfer all thermal and mechanical radial loads between the tubesheets. Additionally, it is understood that the tubes are rigid enough to mutually transfer all mechanical and thermal axial loads between the tubesheets.

RCB-7.153 SPECIAL PRECAUTIONS

RCB-7.154 INTEGRAL DOUBLE TUBESHEETS

FIGURE RCB-7.154

RCB 7.1541 TUBESHEET THICKNESS Calculate the total combined tubesheet thickness (7) per Paragraph RCB-7.13. where

T = Greater of the thickness, inches (mm), resulting from Paragraphs RCB-7.132 or RCB-7.133 using the following variable definitions: Per Paragraph RCB-7.13, inches (mm), using worst case values of shell side or tube side tubesheets at their respective design temperature. Lower of the Code allowable stress, psi (kPa), for either component tubesheet at its respective design temperature. Per Paragraph RCB-7.13, using worst case values of shell side or tube side tubesheets at their respective design temperature.

All other variables are per Paragraph RCB-7.13. Establish the thickness of each individual tubesheet so that t + t I 2 7' and the minimum individual tubesheet thicknesses ( t and t z ) shall be the greater of Paragraphs RCB-7.13 or RCB.7.134, as applicable.

G =

S =

F =

where

t , = Thickness of tube side tubesheet, inches (mm).

t = Thickness of shell side tubesheet, inches (mm).



RCB-7.1542 INTERCONNECTING ELEMENT DESIGN - SHEAR

The radial shear stress (t), psi (kPa), at attachment due to differential thermal expansion of tubesheets shall not exceed 80% of the lower Code allowable stress (S) of either of the tubesheet materials or the interconnecting element at their respective design temperature. The shear is defined as:

FE t E

FE t E

t =: - 5 0 . 8 s

(Metric) t = ---X l o 6 5 0 . 8 s

t , = Thickness of interconnecting element, inches (mm).

where

where

F,=

E l =

E , =

a I =

a2 =

A T , =

A T , =

Force per unit measure due to differential radial expansion, Ibf/in (kN/mm). Modulus of Elasticity of tubesheet 1 at mean metal temperature, psi (kPa). Modulus of Elasticity of tubesheet 2 at mean metal temperature, psi (kPa). Coefficient of thermal expansion for tubesheet 1 at mean metal temperature, inches/inch/ O F (mm/mm/ O C).

Coefficient of thermal expansion for tubesheet 2 at mean metal temperature, inches/inch/ O F (mm/mm/ O C).

Difference in temperature from ambient conditions to mean metal temperature for tubesheet 1, O F (" C).

Difference in temperature from ambient conditions to mean metal temperature for tubesheet 2, O F (" C).

RCB-7.1543 INTERCONNECTING ELEMENT DESIGN - BENDING AND TENSILE The combined stresses from bending due to differential thermal expansion of tubesheets and axial tension due to thermal expansion of tubes shall not exceed 1.5 times the Code allowable stress (S) of the interconnecting element. The combined total stress of interconnecting element (oE), psi (kPa), is given by:

a, = cr8 + o,, 5 1.5s


SECTION 5

58


The stress due to axial thermal expansion of tubes ( 0 T E ) , psi (kPa), is defined as:

where

The stress due to bending caused by differential thermal expansion of tubesheets 0 B , psi (kPa), is defined as:

6MB (3, = 2

t E

(Metric) (3, = 6 M B x 7 l o6 t E

The bending moment is defined as:

F E g M,=- 2

where M,=

g =

aT =

a E =

AT7 =

A T , =

E,=

E E =

A , =

A , =

F T E =

Bending moment per unit measure acting on interconnecting element, inch-pounds per inch (mm-kN/mm). Spacing between tubesheets, inches (mm). The spacing between tubesheets for an integral double tubesheet is left to the discretion of the manufacturer. For other types of double tubesheets, the minimum spacing is determined in accordance with Paragraphs RCB-7.1552 or RCB-7.1562, as applicable. Coefficient of thermal expansion of tubes at mean metal temperature, inches/inch/ O F (mm/mm/ O C).

Coefficient of thermal expansion of interconnecting element at mean metal temperature, inches/inch/ O F (mm/mm/ O C). Difference in temperature from ambient conditions to mean metal temperature for tubes, O F f‘ C). Difference in temperature from ambient conditions to mean metal temperature for interconnecting element, O F (O C). Modulus of Elasticity of tubes at mean metal temperature, psi (kPa).

Modulus of Elasticity of interconnecting element at mean metal temperature, psi (kPa). Total cross sectional area of tubes between tubesheets, square inches (mm2). Total cross sectional area of interconnecting element, square inches (mm2). Resultant force due to the difference in thermal expansion between tubes and element, Ibf (kN).

- - -~ - - - ~ ~ _ _ _ _ _ _ _ _



RCB-7.1544 TUBE STRESS CONSIDERATION - AXIAL STRESS '

The axial stresses in the tubes due to thermal expansion and pressure load shall not exceed the Code allowable stress (S) of the tubes at design temperature. The total combined stress of the tubes (a T)r psi (kPa), is given by:

a = (I, + 0 T T 5 s

The axial stress due to pressure (6 ,), psi (kPa), is defined as:

P n ( G 2 - Nd:) 4 A r

6 , =

where P = Greater of shell side or tube side design pressure, psi (kPa).

G = Per Paragraph RCB-7.33, inches (mm).

N = Number of tubes.

d o = Tube OD between tubesheets, inches (mm).

The stress due to axial thermal expansion of tubes (6 77j, psi (kPa), is defined by:

F T E ( I T T = -

AT

(Metric) F T E 6 (I,, = -x 10

AT

RCB-7.155 CONNECTED DOUBLE TUBESHEETS The tubesheets are connected in a manner which distributes axial load between tubesheets by means of an interconnecting cylinder, The effect of the differential radial growth between tubesheets is a major factor in tube stresses and spacing between tubesheets. It is assumed the interconnecting cylinder and tubes are rigid enough to mutually transfer all mechanical and thermal axial loads between the tubesheets.

FIGURE RCB-7.155

RCB-7.1551 TUBESHEET THICKNESS

Calculate the total combined tubesheet thickness (7) per Paragraph RCB-7.13.



where T = Greater of the thickness, inches (mm), resulting from Paragraphs

RCB-7.132 or RCB-7.133 using variables as defined in Paragraph RCB-7.1541.

Establish the thickness of each individual tubesheet so that t + t 2 T and the minimum individual tubesheet thickness (t and t z ) shall be the greater of Paragraph RCB-7.13 or RCB-7.134, when applicable. where

t , = Thickness of tube side tubesheet, inches (mm).

t , = Thickness of shell side tubesheet, inches (mm).

RCB-7.1552 MINIMUM SPACING BETWEEN TUBESHEETS

The minimum spacing (g), inches,(mm), between tubesheets required to avoid overstress of tubes resulting from differential thermal growth of individual tubesheets is given by:

where

d = Tube OD between tubesheets, inches (mm)

y ~ = Yield strength of the tube material at maximum metal temperature, psi (kPa).

11 f = Differential radial expansion between adjacent tubesheets, inches (mm). (Measured from center of tubesheet to D T L ).

where D J L = Outer tube limit, inches (mm).

RCB-7.1553 INTERCONNECTING ELEMENT DESIGN - AXIAL STRESS

The interconnecting element axial stress ( ( J ~ ~ ) , psi (kPa), due to the thermal expansion of the tubes shall not exceed the Code allowable stress (S) of the interconnecting element at design temperature. The axial stress is defined as:

F T E ( s J T E = - AE

F T E (Metric) Q T E = - X 1 O6

AE

where

( ~ , ~ ~ T - ~ E ~ T E ) ( E T A T ) ( E E A E ) ( E T A T ) + ( E E A E )

F T , =

60 Standards Of The-Ttibular-Exchang-er-lvllanufacturers Association


RCB-7.1554 TUBE STRESS CONSIDERATIONS - AXIAL STRESS

The axial stresses in the tubes due to thermal expansion and pressure load shall not exceed the Code allowable stress (S) of the tubes at design temperature. The total combined stress of tubes (aT), psi (kPa), is given by:

6, = 6, + O T T 1. s

The axial stress due to pressure (a P ) r psi (kPa), is defined as:

P n ( G 2 - N d o 2 ) 4 A r

6, =

where P = Greater of shell side or tube side design pressure, psi (kPa).

G = Per Paragraph RCB-7.13, inches (mm).

N = Number of tubes.

d = Tube OD between tubesheets, inches (mm).

The stress due to axial thermal expansion of tubes (0 TT), psi (kPa), is determined by:

F T E 6,, = -

AT

(Metric) F T E

AT or , = -x l o6

RCB-7.156 SEPARATE DOUBLE TUBESHEETS The tubesheets are connected only by the interconnecting tubes. The effect of differential radial growth between tubesheets is a major factor in tube stresses and spacing between tubesheets. It is assumed that no loads are transferred between the t ubesheets.

FIGURE RCB-7.156



62

RCB-7.1561 TUBESHEET THICKNESS Calculate tube side tubesheet thickness per Paragraph RCB-7.13. Use all variables as defined per TEMA, neglecting all considerations of shell side design conditions. Calculate shell side tubesheet thickness per Paragraph RCB-7.13. Use all variables as defined per TEMA, neglecting all considerations of tube side design conditions.

RCB-7.1562 MINIMUM SPACING BETWEEN TUBESHEETS

The minimum spacing (g), inches (mm), between tubesheets required to avoid overstress of tubes resulting from differential thermal growth of individual tubesheets is given by:

RCB-7.16 FIXED TUBESHEET EFFECTIVE PRESSURE

This paragraph shall apply to exchangers having tubesheets fixed to both ends of the shell, with or without a shell expansion joint except as required or permitted by Paragraph RCB-7.3. Both tubesheets of fixed tubesheet exchangers shall have the same thickness, unless the provisions of Paragraph RCB-7.166 are satisfied. For fixed tubesheet exchangers, the mutually interdependent loads exerted on the tubesheets, tubes, and shell are defined in terms of equivalent and effective design pressures in Paragraphs RCB-7.161 through RCB-7.165 for use in Paragraphs RCB-7.132 and RCB-7.133. These pressures shall also be used (with J = 1) in Paragraphs RCB-7.22, RCB-7.23 and RCB-7.25 to assess the need for an expansion joint. The designer shall consider the most adverse operating conditions specified by the purchaser. (See Paragraph E-3.2.)

RCB-7.161 EQUIVALENT DIFFERENTIAL EXPANSION PRESSURE The pressure due to differential thermal expansion, psi (kPa), is given by:

4 J E s t , ( E ) P,=

( D 0 - 3 t s ) ( 1 + J K F , )

Note: Algebraic sign must be retained for use in Paragraphs RCB-7.163 through RCB-7.166, RCB-7.22 and RCB-7.23.

where J = 1 .O for shells without expansion joints

S,L J = for shells with expansion joints. See Note (1)

S j L + ~ t ( Do - t , ) t , E

S , = Spring rate of the expansion joint, Ibs/inch (kN/mm)

[ 300 t , E , ( ~)'] ' ' ' K L E

F q = 0 . 2 5 + ( F - 0 . 6 )

(Use the calculated value of F or 1 .O, whichever is greater.) F and G are as defined in Paragraph RCB-7.132.



T = Tubesheet thickness used, but not less than 98.5% of the greater of the values defined by Paragraph RCB-7.132 or RCB-7.133. (The value assumed in evaluating F must match the final computed value within a tolerance of f 1.5%) See Note (2).

L = Tube length between inner tubesheet faces, inches (mm). A L = Differential thermal growth (shell - tubes), inches (mm) (See Section 7,

Paragraph T-4.5). L , = Tube length between outer tubesheet faces, inches (mm).

E = Elastic modulus of the shell material at mean metal temperature, psi (kPa). (See Paragraph RCB-1.431). See Note (3).

E , = Elastic modulus of the tube material at mean metal temperature, psi (kPa). (See Paragraph RCB-1.432).

E = Elastic modulus of the tubesheet material at mean metal temperature, psi (kPa). (See Paragraph RCB-1.432).

N = Number of tubes in the shell. D o = Outside diameter of the shell or port for kettle type exchangers, inches (mm). d o = Outside diameter of the tubes (for integrally finned tubes, d o is root diameter of

t = Tube wall thickness (for integrally finned tubes, t , is wall thickness under fin),

t = Shell wall thickness, inches (mm).

fin), inches (mm).

inches (mm).

Notes: (1) J can be assumed equal to zero for shells with expansion joints where

(2) Tubesheets thicker than computed are permissible provided neither shell nor tubes

(3) For Kettle type, are overloaded. See Paragraph RCB-7.2.

ESHL E , = ( 2 L P I ' [ ( 4 L C TP D P ) / ( ( D P + D K IT, 13' [( K T P D P K K 11

where E SH = Elastic modulus of the shell material at mean metal temperature, psi

(kPa). (See Paragraph RCB-1.431). L = Tube length between inner tubesheet faces, inches (mm).

L , = Length of kettle port cylinder, inches (mm).

T , = Kettle port cylinder thickness, inches (mm).

D = Mean diameter of kettle port cylinder, inches (mm).

L , = Length of kettle cylinder, inches (mm).

T , = Kettle cylinder thickness, inches (mm).

D , = Mean diameter of kettle cylinder, inches (mm).

L , = Axial length of kettle cone, inches (mm).

?rC = Kettle cone thickness, inches (mm).

RCB-7.162 EQUIVALENT BOLTING PRESSURE When fixed tubesheets are extended for bolting to heads with ring type gaskets, the extension and that portion of the tubesheets inside the shell may differ in thickness. The extension shall be designed in accordance with Paragraph RCB-7.734. The effect



64

of the moment acting upon the tubesheet extension shall be accounted for in subsequent paragraphs in terms of equivalent tube side and shell side bolting pressures which are defined as:

6.2 Mi

6.2 M2 p B s = F2 G 3

where F and G are defined in Paragraph RCB-7.132.

M = Total moment acting upon the extension under operating conditions, defined

M = Total moment acting upon the extension under bolting-up conditions, defined

by the Code as A4 under flange design, inch-pounds (mm-kN).

by the Code as M I under flange design, inch-pounds (mm-kN).

P B t = Equivalent bolting pressure when tube side pressure is acting, psi (kPa).

P Bs = Equivalent bolting pressure when tube side pressure is not acting, psi (kPa).

RCB-7.163 EFFECTIVE SHELL SIDE DESIGN PRESSURE The effective shell side design pressure is to be taken as the greatest absolute value of the following:

P B s -k Pd 2 or P =

or P = P s ‘ - P B s

where

0.4 J [ 1 . 5 + K ( 1 . 5 + f s > ] - [ (y)( 5- I ) ] ]

1 + J K F , P , ‘ = P ,

P = Shell side design pressure, psi (kPa) (For vacuum design, P is negative). 2

f s = I+($)

G = Inside diameter of the shell, inches (mm).

D , = Maximum expansion joint inside diameter, inches (mm) ( D , = G when no expansion joint is present).

Other symbols are as defined under Paragraphs RCB-7.161 and RCB-7.162



Notes: (1) Algebraic sign of P ’ must be used above, and must be retained for use in

(2) When J = 0, formulae containing P will not control.

(3) Delete the term P B s in the above formulae for use in Paragraph RCB-7.133.

(4) For kettle type, G = port inside diameter.

Paragraphs RCB-7.164, RCB-7.165, RCB-7.166, RCB-7.22 and RCB-7.23.

RCB-7.164 EFFECTIVE TUBE SIDE DESIGN PRESSURE The effective tube side design pressure is to be taken as the greatest absolute value of the following:

o r P = P,’+ P,,

P , ‘ - P,‘+ P,,+ Pd 2

P =

orP= P t ’ - P s d + P B t where

When P ‘ is positive

When P ’ is negative

I 1 + 0 . 4 J K ( 1 . 5 + f t ) 1 +. J K F ,

P,‘= P,

P , = Tube side design pressure, psi (kPa) (For vacuum design, P is negative).

2 i t = ] - ” d, -2 t , ] G = Inside diameter of the shell, inches (mm).

Other symbols are as defined under Paragraphs RCB-7.161, RCB-7.162, and RCB-7.163.

Notes: (1) Algebraic sign of P , ’ must be used above, and must be retained for use in

(2) When J = 0:

Paragraphs RCB-7.165, RCB-7.166, RCB-7.22 and RCB-7.23.

a) Formulae containing P d will not control.

b) When P , and P are both positive the following formula is controlling:

P = P , + “c 2 ( $)2- 1]+ p B t

(3) Delete the term P,, in the above formulae for use in Paragraph RCB-7.133.

(4) For kettle type, G = port inside diameter.

RCB-7.165 EFFECTIVE DIFFERENTIAL DESIGN PRESSURE Under certain circumstances the Code and other regulatory bodies permit design on the basis of simultaneous action of both shell and tube side pressures. The effective differential design pressure for fixed tubesheets under such circumstances is to be taken as the greatest absolute value of the following:


SECTION 5

66

MECHANICAL STANDARDS TEMA CLASS FI C B

P = P,'- P , ' + P B t

or P t ' - P,'+ P B t + P , P =

2

or P = P,,

P B s 4- pci 2 or P =

where

P d , f' B , p B~ p , 'and P i ' are as defined in Paragraphs RCB-7.161, RCB-7.162, RCB-7.163 and RCB-7.164.

Notes:

(1) It is not permissible to use ( P - P ) in place of P , to calculate P in Paragraph RCB-7.763, and it is not permissible to use (P - P ) in place of P to calculate P * in Paragraph RCB-7.164.

(2) When J = 0, the formulae containing P dwill not control.

(3) Delete the terms P B 1 and P Bs in the above formulae for use in Paragraph

'

RCB-7.133.

RCB-7.166 FIXED TUBESHEETS OF DIFFERING THICKNESSES The rules presented in Paragraphs RCB-7.761 through RCB-7.165 and RCB-7.2 are intended for fixed tubesheet exchangers where both tubesheets are the same thickness. Conditions can exist where it is appropriate to use tubesheets of differing thicknesses. These conditions may result from significantly differing elastic moduli and/or allowable stresses. The following procedure may be used for such cases: (1) Separate the design parameters as defined in previous paragraphs for

each tubesheet system by assigning subscripts A and B to each of the following terms:

LasLAandLBwhereL,+LB=2L

F as F,,and F q B

Tas TA and T B

E as E A and E B

Note: The values of M , M , , F , G , A L , L,, D o , t d o , 2 I E ,, E N and S , must remain constant throughout this analysis. If a fixed tubesheet exchanger has different bolting moments at each tubesheet, the designer should use the values of M and M that produce the conservative design.

(2) Calculate T A per Paragraphs RCB-7.161 through RCB-7.165 assuming that both tubesheets have the properties of subscript A and L A = L.



Calculate T per Paragraphs RCB-7.161 through RCB-7.165 assuming that both tubesheets have the properties of subscript Band L E = L. Calculate L A and L as follows: L = L , - T , - T B

L A = 2 L - L B Recalculate T A per Paragraphs RCB-7.161 through RCB-7.165 using the properties of subscript A and L A from step 4. Recalculate T per Paragraphs RCB-7.161 through RCB-7.165 using the properties of subscript Band L from step 4. Repeat steps 4 through 6 until values assumed in step 4 are within 1.5% of the values calculated in step 5 for T A and step 6 for T E .

Round T A and T up to an appropriate increment and recalculate L A and L per step 4. Calculate the shell and tube stresses and the tube-to-tubesheet joint loads per Paragraph RCB-7.2 for each tubesheet system using the appropriate subscripted properties. The shell and tube stresses and tube-to-tubesheet joint loads for each tubesheet system should theoretically be identical. Small differences may exist, however, because of rounding the calculated tubesheet thicknesses in step 8. The tube stress and the tube-to-tubesheet joint loads from the two systems should be averaged before comparing these values to the allowable values as calculated in Paragraph RCB-7.2.

0 * RCB-7.2 SHELL AND TUBE LONGITUDINAL STRESSES - FIXED TUBESHEET EXCHANGERS Shell and tube longitudinal stresses, which depend upon the equivalent and effective pressures determined by Paragraphs RCB-7.161 through RCB-7.164, shall be calculated for fixed tubesheet exchangers with or without shell expansion joints by using the following paragraphs. The designer shall consider the most adverse operating conditions specified by the purchaser. (See Paragraph E-3.2.) Note: The formulae and design criteria presented in Paragraphs RCB-7.23 through RCB-7.25

consider only the tubes at the periphery of the bundle, which are normally the most highly stressed tubes. Additional consideration of the tube stress distribution throughout the bundle may be of interest to the designer under certain conditions of loading and/or geometry. See the "Recommended Good Practice" section of these Standards for additional information.

RCB-7.21 HYDROSTATIC TEST Hydrostatic test conditions can impose excessive shell and/or tube stresses. These stresses can be calculated by substituting the pressures and temperatures at hydrostatic test for the appropriate design pressures and metal temperatures in the paragraphs that follow and in Paragraphs RCB-7.161 through RCB-7.164 where applicable.

RCB-7.22 SHELL LONGITUDINAL STRESS The effective longitudinal shell stress is given by:

C s ( D 0 - t s ) P , * 4 t s

ss =

where c, = 1 .o except as noted below

P , * = P , Note (2)



68

orP,* = P,' Note (2)

or P , * = - P d Note (1)

or P , * = P I + P,'

orP,* = P l - p d

orP,* = P,'-Pd

or P, * = P , + P , ' - Pd

Notes (1) and (2)

Notes (1) and (2)

Note (1)

where P , = P,- P,'

Other symbols are as defined in Paragraphs RCB-7.161, RCB-7.163 and RCB-7.164, using actual shell and tubesheet thicknesses and retaining algebraic signs. Notes:

(1) If the algebraic sign of P * is positive, C, = 0.5.

(2) This formula is not applicable for differential pressure design per Paragraph RCB-7.165.

A condition of overstress shall be presumed to exist when the lar est absolute value of S exceedsJhe Code allowable stress in tension for the shell materii at design temperature, or 90% of ield stress at hydrostatic test, or when the greatest negative value of S .exceeds the Code dowable stress in compression at design temperature.

RCB-7.23 TUBE LONGITUDINAL STRESS - PERIPHERY OF BUNDLE The maximum effective longitudinal tube stress, psi (kPa), at the periphery of the bundle is given by:

C, F , P,* G 2 S f =

4 N t , ( d , - t , )

where C f = 1 .o except as noted below

P,* = P 2 Note (2)

o r P 1 * = -P 3

orP,* = P d

orP,* = P2-P3

orP1* = P2+Pd

o rP f * = - P 3 + P d

o r P f * = P 2 - P 3 + P d Note(1)

Note (2)

Notes (1) and (2)

Notes (1) and (2)

Notes (1) and (2)

where

P , = K - ( f 7 ) fPf

Other symbols are as defined in Paragraphs RCB-7.161, RCB-7.163 and RCB-7.164, using actual shell and tubesheet thicknesses and retaining algebraic signs.



k =

Notes: (1) If the algebraic sign of P , * is positive, C , = 0.5

0.6 for unsupported spans between two tubesheets 0.8 for unsupported spans between a tubesheet and a tube support 1 .O for unsupported spans between two tube supports

(2) This formula is not applicable for differential pressure design per Paragraph RCB-7.165.

A condition of overstress shall be presumed to exist when the largest positive value of S , exceeds the Code allowable stress in tension for the tube material at design temperature, or 90% of yield stress at hydrostatic test, or when the greatest negative value of S exceeds the allowable compressive stress as determined in accordance with Paragraph RCB-7.24.

RCB-7.24 ALLOWABLE TUBE COMPRESSIVE STRESS - PERIPHERY OF BUNDLE The allowable tube compressive stress, psi (kPa), for the tubes at the periphery of the bundle is given by:

Jc2 E , s, =

F , (y kl

when c, 5 - r

where

c,= J"' S Y

S , = Yield stress, psi (kPa), of the tube material at the design metal temperature. (See Paragraph RCB-1.42).

r = Radius of gyration of the tube, inches (mm), given by: r = 0.25Jd0 * + ( d o - 2 t , ) 2 (See Table 0-7).

F = Factor of safety given by:

F , = 3.25 - 0 . 5 F q

Note: F shall not be less than 1.25 and need not be taken greater than 2.0.

Note: The allowable tube compressive stress shall be limited to the smaller of the Code Other symbols are as defined in Paragraph RCB-7.161.

allowable stress in tension for the tube material at the design metal temperature (see Paragraph RCB-1.42) or the calculated value of S .

RCB-7.25 TUBE-TO-TUBESHEET JOINT LOADS - PERIPHERY OF BUNDLE The maximum effective tube-to-tubesheet joint load, Ibs. (kN), at the periphery of the bundle is given by:

n F , P,* G 2 4 N

W , =


SECTION 5

where


P,* = P , Note (1)

o rP2* = - P 3 Note (1)

orP,* = P , - P 3

P and P are as defined in Paragraph RCB-7.23. Other symbols are as defined in Paragraphs RCB-7.161, RCB-7.163 and RCB-7.164, using the actual shell and tubesheet thicknesses.

Note: (1) This formula is not applicable for differential pressure design per Paragraph RCB-7.165.

The allowable tube-to-tubesheet joint loads as calculated by the Code or other means may be used as a guide in evaluating W , . The tubetotubesheet joint loads calculated above consider only the effects of pressure loadings. The tube-to-tubesheet joint loads caused by restrained differential thermal expansion between shell and tubes are considered to be within acceptable limits if the requirements of Paragraph RCB-7.23 are met.

RCB-7.3 SPECIAL CASES Special consideration must be given to tubesheet designs with abnormal conditions of support or loading. Following are some typical examples: (1) Tubesheets with portions not adequately stayed by tubes, or with wide untubed rims. (2) Exchangers with large differences in shell and head inside diameters; e.g. fixed tubesheets with

kettle type shell. (3) The adequacy of the staying action of the tubes during hydrostatic test; e.g., with test rings for

types S and T, or types P and W. (4) Vertical exchangers where weight and/or pressure drop loadings produce significant effects

relative to the design pressures. (5) Extreme interpass temperature differentials. Consideration may also be given to special design configurations and/or methods of analysis which may justify reduction of the tubesheet thickness requirements.

RCB-7.4 TUBE HOLES IN TUBESHEETS

RCB-7.41 TUBE HOLE DIAMETERS AND TOLERANCES Tube holes in tubesheets shall be finished to the diameters and tolerances shown in Tables RCB-7.41 and RCB-7.41 M, column (a). To minimize work hardening, a closer fa between tube OD and tube ID as shown in column (b) may be provided when specified by the purchaser.

Tables RCB-7.42 and RCB-7.42M give permissible tubesheet ligaments, drill drift and recommended maximum tube wall thicknesses.

The inside edges of tube holes in tubesheets shall be free of burrs to prevent cutting of the tubes. Internal surfaces shall be given a workmanlike finish.

RCB-7.42 TUBESHEET LIGAMENTS

*RCB-7.43 TUBE HOLE FINISH



Tube OD

1 I 4

TABLE RCB-7.41 TUBE HOLE DIAMETERS AND TOLERANCES

(All Dimensions in Inches)

Nominal Under Nominal Under Diameter Tolerance Diameter Tolerance

0.259 0.004 0.257 0.002 1

318

112

Nominal

. ..

0.384 0.004 0.382 0.002 0.002 0.007

0.510 0.004 0.508 0.002 0.002 0.008

Standard Fit ( 4

518

314

7f8 1

1-114

Special Close Fit (b)

0.635 0.004 0.633 0.002 0.002 0.010

0.760 0.004 0.758 0.002 0.002 0.010

0.885 0.004 0.883 0.002 0.002 0.010

1.012 0.004 1.010 0.002 0.002 0.010

1.264 0.006 1.261 0.003 0.003 0.010 -~

1-112 1.518

2 2.022

Over Tolerance: 96% of tube holes must meet value in column (c). Remainder may not exceed

0.007 1.514 0.003 0.003 0.010

0.007 2.018 0.003 0.003 0.010 I Nominal Tube Hole Diameter and Under Tolerance

Standard Fit Special Close Fit Nominal (a) (b)

Tube OD Nominal Under Nom i n al Under Diameter Tolerance Diameter Tolerance

6.4 6.58 0.10 6.53 0.05

9.5 9.75 0.10 9.70 0.05

12.7 12.95 0.10 12.90 0.05

15.9 16.13 0.10 16.08 0.05

19.1 19.30 0.10 19.25 0.05

22.2 22.48 0.10 22.43 0.05

25.4 25.70 0.10 25.65 0.05

31.8 32.1 1 0.15 32.03 0.08

38.1 38.56 0.18 38.46 0.08 50.8 51.36 0.18 51.26 0.08

-----

Over Tolerance: 96% of tube holes must meet value in column (c). Remainder may not exceed

value in column (d)

(c) ( 4 0.05 0.18

0.05 0.18

0.05 0.20 0.05 0.25

0.05 0.25

0.05 0.25

0.05 0.25

0.08 0.25

0.08 0.25

0.08 0.25


SECTION 5

1

0.025 0.083


1-112 2 2-112 3 4 5 6 _ _ -- -- 0.025 0.025 0.025 -

0.077 0.070 0.064 -- -- -- --

TABLE RCB-7.42 TABLE OF TUBESHEET LIGAMENTS AND RECOMMENDED HEAVIEST TUBE GAGES

(All Dimensions in Inches)

0.087 0.119

318 I 112 I 1.33 17/32 1.42

0.083 0.079 0.075 0.070 0.062 -- -- 0.114 0.110 0.106 0.102 0.093 0.085 0.076

21/32 18 16 16

15 14 14

1-1/8

0.510 0.115 0.146 0.178

0.635 0.146 0.178 0.240

1-3/32 1.25 7/8 I 1-118 I 1.29

0.089 0.120 0.151

0.111 0.142 0.205

1-3/16 1.36 1-114 1.43

1-114 1.25

0.085 0.082 0.079 0.076 0.069 0.063 -- 0.117 0.113 0.110 0.107 0.107 0.094 0.088 0.148 0.145 0.142 0.138 0.132 0.126 0.119

0.109 0.106 0.103 0.101 0.096 0.091 0.086 0.140 0.137 0.135 0.132 0.127 0.122 0.117 0.202 0.200 0.197 0.195 0.189 0.184 0.179

1114 1-9/16 1.25

~

0.206 0.269 0.331

-

3 - d

- 1/16 1 /8

118

1 /a

- 5/32

5/32 3/16

5/32 3/16

3/16

5/16

7/32

5/16

- - 114

1 /4

318

1 I 4

318

1 I 4

318

318

1 /2

-

-

- 5/16

5/16 - - - -

0.205 0.203 0.201 0.199 0.195 0.192 0.188 0.267 0.265 0.263 0.262 0.258 0.254 0.251 0.330 0.328 0.326 0.324 0.320 0.317 0.313

Gage BWG

0.205 0.267 0.330

+ 18

0.203 0.202 0.200 0.198 0.195 0.192 0.189 0.266 0.264 0.263 0.261 0.258 0.255 0.251 0.328 0.327 0.325 0.323 0.320 0.317 0.314

Nomin- al

Liga- ment Width

0.054 0.1 16

0.116 0.147

0.266

0.325 --

0.265 0.263 0.262 0.261 0.258 0.256 0.253

0.324 0.323 0.322 0.321 0.318 0.316 0.314

0.446 0.445 0.444 0.443 0.442 0.440 0.438

13 0.760 0.178 12 I 1 0.240 12 0.303 12 I I 0.365 !i 1 0.885 1 0.209

0.240 0.303 0.365

1.012 0.238 Lo 1 1 0.301 9 0.363

9

8

6

Minimum Std. Ligaments (96% of ligaments must equal or exceed values tabulated below)

Minimum 'ermissible Ligament

Width

0.025 0.060

0.060 0.075

0.060 0.075 0.090

0.075 0.090 0.120

0.090 0.120 0.150 0.185

0.105 0.120 0.150 0.185

0.120 0.150 0.185

0.150

0.180

0.250

Notes: The above table of minimum standard ligaments is based on a ligament tolerance not exceeding the sum of twice the drill drift tolerance plus 0.020 for tubes less than 5 / 8 OD and 0.030 for tube holes 5/8" OD and larger. Drill drift tolerance = 0.0016 (thickness of tubesheet in tube diameters), inches

* RC 8-7.5 TU BE-TO-TU BESHEET J 01 NTS RCB-7.51 EXPANDED TUBE-TO-TUBESHEET JOINTS

Expanded tube-to-tubesheet joints are standard.

RB-7.511 LENGTH OF EXPANSION Tubes shall be expanded into the tubesheet for a length no less than 2" (50.8 mm) or the tubesheet thickness minus 1 /8" (3.2 mm), whichever is smaller. In no case shall the expanded portion extend beyond the shell side face of the tubesheet. When specified by the purchaser, tubes may be expanded for the full thickness of the tubesheet.

Tubes shall be expanded into the tubesheet for a length no less than two tube diameters, 2" (50.8 rnrn),, or the tubesheet thickness minus 1/8" (3.2 mm), whichever is smaller. In no case shall the expanded portion extend beyond the shell side face of the tubesheet. When specified by the purchaser, rubes may be expanded for the full thickness of the tubesheet.

C-7.511 LENGTH OF EXPANSION



Tube Dia.

do

6.4

9.5

Tube Pitch P

7.94 9.53

13.49 12.70

TABLE RCB-7.42 M TABLE OF TUBESHEET LIGAMENTS AND RECOMMENDED HEAVIEST TUBE GAGES

34.9:

1.25 I 1.59 I 1.50 3.18

2.; I 6.579

1.33 3 17 1.42 I 3:96 I ;: I 9'754

1.25 3.18 18 12.954 1.31 3.97 1.37 I 4.76 1 ;E 1 1.25 3.96 15 16.125 1.30 4.76 14 1.40 6.35 14 1.25 4.76 13 19.304

1.25 5.55 12 22.475 1.29 I 6.35 I 12 1

l o I 1.36 793 1.43 1 9:52 I 10 1.25 6.35 10 25.705 1.31 7.94 9 1.38 9.53 9 1.25 7.94 9 32.10C 1.25 I 9.53 I 1::::; 1.25 12.70

iotes: The above table of minimum standard drift tolerance plus 0.51mm for tubes les Drill drift tolerance = 0.041 (thickness of

(All Dimensions in mm)

Minimum Std. Ligaments (96% of ligaments must equal or exceed values tabulated below)

Nomin- al

Liga- ment Width Tubesheet Thickness

Minimum Permissible Ligament ! Width

25.4 I 38.1 I 50.8 1 63.5 I 76.2 I 101.6 I 127.0 I 152.4 I 1.361 0.635 0.635 0 635 0 635 - 0.635 I 2.951 12.1081 1.956 I 11778 I 1:626 I - 1 1 1 1 I 1 1.524

2.946 2 210 2 108 2 007 1 905 1 778 1 575 3.736 I 3:023 I 2:896 I 21794 I 2:692 1 2:591 I 2:362 I 2.159 I 1.930 1 1.524 1

1.905

2.926 2.261 2.159 2.083 2.007 1.930 1.753 1.600 - 1.524 3.716 3.048 2.972 2.870 2.794 2.718 2.565 2.388 2.235 1.905 4.506 3.835 3.759 3.683 3.607 3.505 3.353 3.200 3.023 2.286

3.711 2.819 2.769 2.692 2.616 2.565 2.438 2.311 2.184 1.905 4.511 3.607 3.556 3.480 3.429 3.353 3.226 3.099 2.972 2.286 6.101 5.207 5.131 5.080 5.004 4.953 4.801 4.674 4.547 3.048

4.506 3.632 3.581 3.531 3.480 3.429 3.302 3.200 3.099 2.286 6.096 5.232 5.182 5.105 5.055 5.004 4.902 4.807 4.674 3.048 7.686 6.807 6.756 6.706 6.655 6.604 6.477 6.375 6.274 3.810 9.276 8.407 8.357 8.280 8.230 8.179 8.077 7.976 7.849 4.699

5.301 4.445 4.394 4.343 4.318 4.267 4.166 4.064 3.988 2.667 6.101 5.232 5.207 5.156 5.105 5.055 4.953 4.877 4.775 3.048 7.681 6.833 6.782 6.731 6.680 6.655 6.553 6.452 6.375 3.810 9.271 8.407 8.382 8.331 8.280 8.230 8.128 8.052 7.950 4.699

I

7.584 6.756 6.731 6.680 6.655 6.629 6.553 6.502 I 6.426 3 . 8 i O 9.073 8.255 8.230 8,204 8.179 8.153 8.077 8.026 I 7.976 4.572 12.141 I - ~11.328~11.303~11.278)11.252~11.227~11.176~11.125~ 6.350 I gaments is based on a ligament tolerance not exceeding the sum of twice the drill than 15.9mrn OD and 0.76mm for tube holes 15.9mm OD and larger. rbesheet in tube diameters), rnrn.

RCB-7.512 CONTOUR OF THE EXPANDED TUBE The expanding procedure shall be such as to provide substantially uniform expansion throughout the expanded portion of the tube, without a sharp transition to the unexpanded portion.

Tubes shall be flush with or extend by no more than one half of a tube diameter beyond the face of each tubesheet, except that tubes shall be flush with the top tubesheet in vertical exchangers to facilitate drainage unless otherwise specified by the purchaser.

RB-7.513 TUBE PROJECTION

RCB-7.52 WELDED TUBE-TO-TUBESHEET JOINTS

When both tubes and tubesheets, or tubesheet facing, are of suitable materials, the tube joints may be welded.

RCB-7.521 SEAL WELDED JOINTS When welded tube joints are used for additional leak tightness only, and tube loads are carried by the expanded joint, the tube joints shall be subject to the rules of Paragraphs RCB-7.4 through RCB-7.51.



74

RCB-7.522 STRENGTH WELDED JOINTS When welded tube joints are used to carry the longitudinal tube loads, consideration may be given to modification of the requirements of Paragraphs RCB-7.4 through RCB-7.51. Minimum tubesheet thicknesses shown in Paragraphs R-7.131, C-7.131 and B-7.131 do not apply.

RCB-7.523 FABRICATION AND TESTING PROCEDURES Welding procedures and testing techniques for either seal welded or strength welded tube joints shall be by agreement between the manufacturer and the purchaser.

RCB-7.53 EXPLOSIVE BONDED TUBE-TO-TUBESHEET JOINTS Explosive bonding and/or explosive expanding may be used to attach tubes to the tubesheets where appropriate. Consideration should be given to modifying the relevant parameters (e.g., tube-to-tubesheet hole clearances and ligament widths) to obtain an effective joint.

R-7.6 TUBESHEET PASS PARTITION GROOVES Tubesheets shall be provided with approximately 3/16" (4.8 mm) deep grooves for pass partition gaskets.

CB-7.6 TUBESHEET PASS PARTITION GROOVES For design pressures over 300 psi (2068 kPa), tubesheets shall be provided with pass partition grooves approximately 3/16" (4.8 mm) deep, or other suitable means for retaining the gaskets in place.

RCB-7.7 TUBESHEET PULLING EYES In exchangers with removable tube bundles having a nominal diameter exceeding 12" (305 mm) and/or a tube length exceeding 96" (2438 mm), the stationary tubesheet shall be provided with two tapped holes in its face for pulling eyes. These holes shall be protected in service by plugs of compatible material, Provision for means of pulling may have to be modified or waived for special construction, such as clad tubesheets or manufacturer's standard, by agreement between the manufacturer and the purchaser.

RB-7.8 CLAD AND FACED TUBESHEETS The nominal cladding thickness at the tube side face of a tubesheet shall not be less than 5/16" (7.8 mm) when tubes are expanded only, and 1 /8" (3.2 mm) when tubes are welded to the tubesheet. The nominal cladding thickness on the shell side face shall not be less than 3/8" (9.5 mm). Clad surfaces, other than in the area into which tubes are expanded, shall have at least 1 /8" (3.2 mm) nominal thickness of cladding.

C-7.8 CLAD AND FACED TUBESHEETS The nominal cladding thickness at the tube side face of a tubesheet shall not be less than 3/16" (4.8 mm) when tubes are expanded only, and 1 /8" (3.2 mm) when tubes are welded to the tubesheet. The nominal cladding thickness on the shell side face shall not be less than 3/8" (9.5 mm). Clad surfaces, other than in the area into which tubes are expanded, shall have at least 1 /8" (3.2 mm) nominal thickness of cladding.



RCB-8 FLEXIBLE SHELL ELEMENTS This paragraph shall apply to fixed tubesheet exchangers which require flexible elements to reduce shell and tube longitudinal stresses and/or tube-to-tubesheet joint loads. Light gauge bellows type ex ansion joints within the scope of the Standards of the Expansion Joint Manufacturers Association (EJMAPare not included within the purview of this paragraph. The analysis contained within these paragraphs is based upon the equivalent geometry used in "Expansion Joints for Heat Exchangers" by S. Kopp and M. F. Sayer; however, the formulae have been derived based upon the use of plate and shell theory modified to account for the stiffness of the knuckle radii, when used. Flanged-only and flanged-and-flued types of expansion joints are examples of flexible shell element combinations. The designer shall consider the most adverse operating conditions specified by the purchaser. (See Paragraph E-3.2.)

RCB-8.1 APPLICATION INSTRUCTIONS AND LIMITATIONS The formulae contained in the following paragraphs are applicable based upon the following assumptions:

Applied loadings are axial. Torsional loads are negligible. The flexible elements are sufficiently thick to avoid instability. The flexible elements are axisymmetric. All dimensions are in inches (mm) and all forces are in pounds (kN). Poisson's ratio is 0.3.

RCB-8.11 CALCULATION SEQUENCE The sequence of calculation shall be as follows:

(1) Select a geometry for the flexible element per Paragraph RCB-8.21. (2) Determine the effective geometry constants per Paragraph RCB-8.22. (3) Calculate the element flexibility factors per Paragraph RCB-8.3. (4) Calculate the element geometry factors per Paragraph RCB-8.4. (5) Calculate the stiffness multiplier per Paragraph RCB-8.5 (6) Calculate the equivalent flexible element stiffness per Paragraph RCB-8.6. (7) Calculate the induced axial force per Paragraph RCB-8.7 for each condition as

(8) Calculate the flexible element moments and stresses per Paragraph RCB-8.8. (9) Compare the flexible element stresses to the appropriate allowable stresses per

shown in Table RCB-8.7.

the Code, for the load conditions as noted in step 7.

(10) Repeat steps 1 through 9 as necessary.

RCB-8.12 CORROSION ALLOWANCE The shell flexible elements shall be analyzed in both the corroded and uncorroded conditions.

RCB-8.13 HYDROSTATIC TEST CONDITIONS The shell flexible elements shall be evaluated for the hydrostatic test conditions.

RC 8-8.2 GEOMETRY D E F IN IT1 ON The geometry may be made up of any combination of cylinders and annular plates with or without knuckle radii at their junctions.

RCB-8.21 PHYSICAL GEOMETRY CONSTANTS Figure RCB-8.21 defines the nomenclature used in the following paragraphs based upon nominal dimensions of the flexible elements.



FIGURE RCB-8.21

1 , 1 0 1 0

I and 1 ,are the lengths of the cylinders welded to single flexible shell elements. When two flexible shell elements are joined with a cylinder, the applicable cylinder length, I or I , used for calculation with the FSE shall be half the actual cylinder length. The applicable cylinder length, I and 1 shall be 0 when a cylinder is not attached.

NOTE: All dimensions shown in Figure RCB-8.21 are in inches (mm).

RCB-8.22 EFFECTIVE GEOMETRY CONSTANTS Figure RCB-8.22 defines the nomenclature used in the following paragraphs based upon the equivalent flexible element model.

FIGURE RCB-8.22

t o 'f


where

t , =


t if the flexible element has a knuckle radius at the inside junction, inches (mm)

t if the flexible element does not have a knuckle radius at the inside junction, inches (mrn)

t if the flexible element has a knuckle radius at the outside junction, inches (mm)

t if the flexible element does not have a knuckle radius at the outside junction, inches (mm)

t b = 1 G + t ,

2 a=- , inches (mrn)

inches (mm)

h = b - a , inches (mm)

t E I, = f a + r a + - 2 , inches (mm)

T o = i-, + 0.5tE r b = rb + 0.5tE K = Stiffener multiplier (See Paragraph RCB 8.5)

Y n = l a + 1 ,

, inches (mm) , inches (mm)

, inches (mm) Note: Cylindrical sections beyond the limit, y , = 2 m, need only meet the Code requirements for cylinders. Note: Cylindrical sections beyond the limit, y b = z&, need only meet the Code requirements for cylinders.

r , , r b , f , , f b , 1 , and 1 are indicated in Figure RCB-8.21.

Y b = I b + l o , inches (mm)

G , 0 D , t

RCB-8.3 ELEMENT FLEXIBILITY FACTORS The effective flexibility factors are given by:

1.285 radians/inch (radianslmm)

1 ,285 radians/inch (radians/rnm)

p a = Jat,

D, = 0.0916E.t. 3, inch-pounds

Metric, D , = 0.0916€,t, 3x10-6 , mrn-kN

Db=0.0916Ebtb 3 , inch-pounds

Metric, D’b=O.O916€btb 3X10-6, mm-kN



E b =

78

E if the flexible element has a knuckle radius at the outside junction, psi (kPa) E , if the flexible element does not have a knuckle radius at the outside junction,

D E = O . O 9 1 6 E E t g 3 , inch-pounds

Metric, D E = 0 . 0 9 1 6 E ~ t E 3 X 1 0 - 6 , mm-kN

0, = p a y a

0 b = p b Yb

for the inner cylinder, radians

for the outer cylinder, radians

j , = s i n R s i n h R

j , = cosRcosh R . 2 2 z = i l + J 2

k , = s i n h R+ s i n R coshSZ+ COSSZ

k , = k ,

k , cosh R - cos SZ

k ,

s inh SZ - s i n R k, =

k, =

where

These values must be calculated for Ra at the inner cylinder as well as R b at the outer cylinder.

E = Modulus of elasticity of the inner cylinder, psi (kPa)

E = Modulus of elasticity of the outer cylinder, psi (kPa)

E = Modulus of elasticity of the flexible shell element, psi (kPa)

E if the flexible element has a knuckle radius at the inside junction, psi (kPa) E if the flexible element does not have a knuckle radius at the inside junction, psi (kPa)

RCB-8.31 CYLINDER-TO-CYLINDER FLEXIBILITY FACTORS

The cylinder-to-cylinder flexibility factors, e ,and e are given by the following:

at the inside junction - Note: If there is no outer cylinder at the outside junction

e , = e e b = e e b = 1

la j b c , =- c,=-

E a C,=- Es

Calculate C + , C 5 , C 6 , C 7 and C with the appropriate values of C , C and C for the inside and outside junction.



when C is less than I .O

0.338172 0.0366351 - 2 C,=-O.364661+

c2 c2 1.01 164 0.122627 -

2 C,=- 1.06871 +

c2 c2

C, = 0.0696709+ 1 .76415C2-5.46103C2

C7=-0.142734+0.918656C2-2.00749C2

when C is greater than or equal to 1 .O

3.37310- 1.707962C2+0.226216C2 C, =

1000

C,= -0.403287+ 0.320037C~-0.0307508C2

C,=-0.684978+0.582549C~-0.0547812C2

C, = -0.20 1334 + 0.168201 C2 - 0.01 57280C,

and

e = 2.7 18"

Notes: (1) When C is less than 0.4, C shall be set equal to 0.4.

(2) When C and C are both equal to 1 .O, e shall be set equal to 1 .O.

RCB-8.4 ELEMENT GEOMETRY FACTORS Calculations for the stiffness and stresses are dependent upon the flexible element geometry factors given by:

Note: kvalues are evaluated using -Ra for the inner cylinder.

Note: kvalues are evaluated using SL ,for the outer cylinder.

-ac(0,769+ 1 .428d2) DE

x , =

2.2ac d 2 DE

X 2 =



-a2[1 .538+ l r ~ ( d ) { 2 + ~ ( 2 + 3 . 7 1 4 d ~ ) } ] X 3 =

408

-2.2bc X 4 =

DE

bc(0.769d2+ 1.428) DE

x s =

- a b ( 1.538+ 5 .714c ln (d ) ) X 6 =

4 D E

X = ( X I - Y 1 > ( X S + Y 2 ) - x Z x 4

x 2 x 6 - x 3 x 5 - x 3 Y 2 x7 = X

g l =0.385a2+ 1.429cb21n(d)

g2=( -0 .385- 1 .429cln(d))b2

g 3 = o . z s , b 2 ( F+ 3 . 7 1 4 ~ ( l n ( d ) ) ~

m i = 0.51 - 0.635g2 + g *

m2=0.635(1 - g 2 ) + g *

rn3= 2.357g2+3.714g*

aandbaredefined in Paragraph RCB-8.22andpa, P b , D , , D b , D E , ea, e b , k l , k 2 a n d k3

are defined in Paragraph RCB-8.3.

where

00 Standarlds Of The Tubular Exctianger-ManufacturWs-Association


RCB-8.5 STIFFNESS MULTIPLIER

Y a Yb ‘’a “ b r , a r * b G Compute the ratios , z, c, r, , -and -

t €

RCB-8.51 If y a / G L 0.075, y a = 1 , If y a / G < 0.075, calculate y a per the formula given below.

If y / G 2 0,075, y = 1 . If y b / G < 0.075, calculate y per the formula given below.

y,= 0.961 - 1 1 .293(y,/G)+450.903(y,/G)2-5647(y,~G)3+23140(y,~G)4

RCB-8.52 If both r ,and r b are present, Fig. RCB-8.21 (a) and r = r b , determine value of mfrOm Figure RCB-8.51 and calculate the term, K , according to the following equations:

i7 For - < 1 6 0 , m = 4.30 ( G / t )-0.287

t €

G For-> 160 ,== 2.92(G/tE)-0.2”

t E

The final stiffness multiplier is represented by the product, K = a m y a y b .

RCB-8.53 If both r ,and r b are present, Fig. RCB-8.21 (a), but not equal, determine m RCB-8.52 using r ’ b , m from Fig. RCB-8.51 using r ’ n , and m o2 from Figure RCB-8.52 using r ‘ n . Calculate K as shown in Paragraph RCB-8.52 above.

The final stiffness multiplier is represented by the product,

from Fig.

a m m o l Y a Y b K = m02

RCB-8.54 If only r b is present, Fig. RCB-8.21 (b) , determine m from Figure RCB-8.52 and calculate the term, h , according to the following equations:

The final stiffness multiplier is represented by the product, K = h rn v a y b

RCB-8.55 If only r , is present, Fig. RCB-8.21 (c) determine rn from Figure RCB-8.51 using r ’a and calculate 0~ , from Paragraph RCB-8.52. Determine m ,,from Figure RCB-8.52 using r ’ b = r ‘a and calculate, h , from Paragraph RCB-8.54.

The final stiffness multiplier is represented by the product,

K = amhmoyayb h m , - a m + ~ m h m o

RCB-8.56 If both Faand T t , equal 0 , Fig. RCB-8.21 (d), K = y o Y b .


3.000

2.800

2.600

2,400

2.200 8

d 1'800 1.600 rn

1,400

1.200

1.000

Ratios not within the range of the r/t and r/h values shown are considered outside the scope of this analysis. --

0 0.05 0.1 0.15 0b2 0.25 0.3 0.35 Ob4 0.45 0.5

r/h

FIGURE RCB-8.51 Stiffness Multiplier as a Function of Flexible Shell Element Dimensionless Parameters

(Inner and Outer Knuckle Radii Equal)

2.000

1.900

1.800 N

G - 1.700

G E" 1,600

4

vl 1.300

1.200

1,100

1.000

FIGURE RCB-8.52 Stiffness Multiplier as a Function of Flexible Shell Element Dimensionless Parameters (No Inner Knuckle)

r/t = 8

r/t = 7

r/t = 6

r/t = 5

rlt = 4

r/t = 3.5

r/t = 3

r/t = 2.5

v)

z 0 m

oi) w


Differential Expansion Only

Shell side Pressure Only, Note (1)

84

0 0 pd

0 P,' 0

RCB-8.6 EQUIVALENT FLEXIBLE ELEMENT STIFFNESS When there is only one flexible shell element (See Paragraph RCB-8.2) in a shell, the spring rate, Ibs/inch (kN/mm), is given by:

2naDE K x7 q 1 .+ x8 4 2 + q 3

S I E =

where the terms are defined in Paragraphs RCB-8.22, RCB-8.3, RCB-8.4, and RCB-8.5. When two or more flexible elements are used in a shell, the overall effective spring rate of the system of flexible elements is given by:

-

Tube side Pressure Only, Note (1)

Shell side Pressure + Tube side Pressure

Shell side Pressure Only t Differential Expansion, Note (1)

1

' , E l S ~ E 2 S , E n

1 1 -+- . I . . . + -

PI 0 0

P , P,' 0

0 Ps' p d

where

s = Overall effective spring rate, Ibs/inch (kN/mm), as used in Paragraph RCB-7.161

s j E 2 . . . s j E n = Respective spring rates of each flexible shell element, calculated individually from the above formula, Ibs/inch (kN/mm) S j ~ l 9

Note: A single convolute consists of two flexible shell elements.

Tube side Pressure Only t Differential Expansion, Note (1)

Shell side Pressure + Tube side Pressure + Differential Expansion

RCB-8.7 INDUCED AXIAL FORCE

p1 0 p d

P P , ' P d

The calculation of the flexible shell element stresses is contingent upon calculating an induced axial force acting on each element. This axial force on the inner shell circumference shall be calculated for each condition as described in Paragraphs RCB-8.11 through RCB-8.13 and is given by:

a P , * 2

F = - , Ibs./inch a x

aP,* (Metric) Fa, = - x ~ o - ~ ,kN/mm

2

where P,* = P I +- P s ' - P d and P I = P , - P, '

TABLE RCB-8.7 F a x PARAMETER VARIATIONS

Notes: (1) This condition is not applicable for differential pressure design per Paragraph RCB-7.165. (2) a is defined in Paragraph RCB-8.22.

Standards-f The Tubular Exchanger Manufacturers Association


(3) Other symbols are as defined in Paragraphs RCB-7.161, RCB-7.163 and RCB-7.164, using actual shell and tubesheet thicknesses for each condition under consideration per Paragraphs RCB-8.11 through RCB-8.13. ALGEBRAIC SIGNS MUST BE RETAINED.

RCB-8.8 FLEXIBLE ELEMENT MOMENTS AND STRESSES The following paragraphs provide the formulae to calculate the predicted stress levels in each flexible element. Each flexible element configuration will have a unique set of stresses for each condition analyzed.

RCB-8.81 MOMENTS AT THE JUNCTIONS The stresses in the annular flat plate and the cylindrical portions of a flexible element are dependent upon the moments, inch-lbs per inch (mm-kN per mm) of circumference, at the inside and outside junctions. The moments are given by:

X M a =

where

P , a 2 - 0 . 3 a F a , z, = E a t ,

P , b - 0.3( a F a w + ( by) P , ) z,= E b t b

P , b 3 eb=- ( - 2 m 2 - m 3 + 0.5-g2) 8DE

P , = Shell side design pressure, psi &Pa), for the condition under consideration

F (including 0 or negative value if vacuum, as applicable)

under consideration = The term as calculated in Paragraph RCB-8.7 dependent upon the condition

k and k = The terms as calculated in Paragraph RCB-8.3, using 0 bat the Outer cylinder

The remaining terms are as defined in Paragraphs RCB-8.22, RCB-8.3 and RCB-8.4.

RCB-8.82 ANNULAR PLATE ELEMENT STRESSES The annular plate meridional bending stress, psi (kPa), shall be calculated for each condition specified in Paragraphs RCB-8.11, RCB-8.12 and RCB-8.13 from the following formula:

A2 A 3 r 2 + A 4 1 n



A 3 = 0 . 2 0 6 P ,

A,= 0.65a(Fa,- 0 .5aPs )

under consideration.

(including 0 or negative value if vacuum, as applicable).

inches (mm).

F a x = The term as calculated in Paragraph RCB-8.7 dependent upon the condition

P, = Shell side design pressure, psi (kPa), for the condition under consideration

r = Radial distance, from the shell centerline to the point under consideration,

The remaining terms are as defined in Paragraphs RCB-8.22, RCB-8.4 and RCB-8.81. Note:

(1) S mbp = S b calculated for the shell side pressure only condition.

(2) S mbd = S b calculated for the differential expansion only or tube side pressure only

(3) S = S bcalculated for all conditions as specified in Table RCB-8.7.

(4) Scmp , Smmp and Smmd as defined by the Code, are negligible for the annular plate element within the scope of Paragraph RCB-8.

(5) The maximum annular plate stress will be located where:

condition.

‘ l i 4 A 3

or r = a

or r = b

RCB-8.83 CYLINDRICAL ELEMENT STRESSES The circumferential membrane stresses, psi (kPa), in the cylinders shall be calculated for each condition specified in Paragraphs RCB-8.17, RCB-8.12 and RCB-8.13 from the following formula:

where

u 1 = P ( Y - x )

u 2 = B , s i n ( u , ) s inh(u ) + B , cos( u 1 ) cosh (u )

x = The distance under consideration, as shown in Figure RCB-8.22, inches (mm)

The remaining terms are as defined in Paragraphs RCB-8.21, RCB-8.22, RCB-8.3 and RCB-8.7.

86 Standards Of The Tubular E n g er Manu f ac%re rs Association


where For the inner cylinder

r = a For the outer cylinder

r = b

t = t ,for ( y ,, - x) < I , t= to fo r (yb -X><l ,

t = t.for(y, - x) > 1 , t = b for ( y b - x > > la t=smalleroft,or t , for(y,-x)= 1 , i = smaller of t b or t ,, for

( Y b - X ) = ‘0

E = E , E = E b

e = e , e = e b

Note: (1) Scmp = S calculated for the shell side pressure only condition.

(2) S cmd = S calculated for the differential expansion only or tube side pressure only condition.

(3) Scmpd = S, calculated for the combined pressure and differential expansion

(4) The maximum value of S will be located where x = y ,, or x = 1 ,for the inner condition.

cylinder and where x = y b or x = I b for the outer cylinder.

RCB-8.84 MAXIMUM CYLINDER STRESS FOR CYCLE LIFE CALCULATIONS The maximum stress, psi (kPa), for a particular set of conditions, for use in the evaluation of cycle life is given by:

where F is defined in Paragraph RCB-8.83

For the inner junction and

M = M ,

t = the smaller of t or t a

For the outer junction . . M = M ,

t = the smaller of t or t b


SECTION 5

Nominal Size Less than 24

24 to 60 (610)

(61 0-1 524)

61 to 100 (1 549-2540)


Carbon Steel Alloy Material 318 1 /4 (9.5) (6.4) 1 12 3/8

(12.7) (9-5)

1 /2 (12.7)

518 (1 5.9)

Note: (1) A positive value of M establishes a compressive stress in the outer fiber of the

(2) S,( is a possible outer limit for establishing a stress range.

(3) S for the cylindrical element is equal to S (.

cylinder under consideration.

RCB-8.9 ALLOWABLE STRESSES The allowable flexible element stresses shall be as defined by the Code, using an appropriate stress concentration factor for the geometry under consideration.

RCB-8.10 MINIMUM THICKNESS The minimum thickness of flexible shell elements shall be as determined by the rules of Paragraphs RCB-8.1 throu h RCB-8.9. However, in no case shall the thickness in the uncorroded condition be less than 1/8"73.2 mm) for nominal diameters 18" (457 mm) and smaller, 3/16" (4.8 mm) for nominal diameters 19" (483 mm) through 30" (762 mm), or 114" (6.4 mm) for nominal diameters greater than 30" (762 mm).

RCB-9 CHANNELS, COVERS, AND BONNETS

RCB-9.1 CHANNELS AND BONNETS

R-9.11 MINIMUM THICKNESS OF CHANNELS AND BONNETS Channel and bonnet thickness is determined by the Code design formulae, plus corrosion allowance, but in no case shall the nominal thickness of channels and bonnets be less than the minimum shell thicknesses shown in Table R-3.13. The nominal total thickness for clad channels and bonnets shall be the same as for carbon steel channels.

CB-9.11 MINIMUM THICKNESS OF CHANNELS AND BONNETS Channel and bonnet thickness is determined by the Code design formulae, plus corrosion allowance, but in no case shall the nominal thickness of channels and bonnets be less than the minimum shell thicknesses shown in Table CB-3.13. The nominal total thickness for clad channels and bonnets shall be the same as for carbon steel channels.

RCB-9.12 MINIMUM INSIDE DEPTH For multipass channels and bonnets the inside depth shall be such that the minimum cross-over area for flow between successive tube passes is at least equal to 1.3 times the flow area through the tubes of one pass. When an axial nozzle is used, the depth at the nozzle centerline shall be a minimum of one-third the inside diameter of the nozzle.

RCB-9.13 PASS PARTITION PLATES

88 ards Of The Tubular E ~ h ~ ~ ~ ~ ~ ~ ~ ~ n u f ~ c t u i e r s - A s s o c i a t i o n


RCB-9.132 PASS PARTITION PLATE FORMULA

where t = Minimum pass partition plate thickness, inches (mm)

B = Table value (linear interpolation may be used)

g = Pressure drop across plate, psi (kPa)

S = Code allowable stress in tension, at design metal temperature, psi (kPa)

b = Plate dimension. See Table RCB-9.132, inches (mm)

PASS PARTITION DIMENSION FACTORS TABLE RCB-9.132

Three sides fixed One side simply supported

a / b 0.25 0.50 0.75 1 .o 1.5 2.0 3.0

B 0.020 0.081 0.173 0.307 0.539 0.657 0.718

Long sides fixed Short sides simply

supported

a / b B 1 .o 0.41 82 1.2 0.4626 1.4 0.4860 1.6 0.4968 1.8 0.4971 2.0 0.4973 03 0.5000

Short sides fixed Long sides simply supported

a / b 1 .o 1.2 1.4 1.6 1.8 2.0 W

B 0.4182 0.5208 0.5988 0.6540 0.691 2 0.7146 0.7500

RCB-9.133 PASS PARTITION WELD SIZE The pass partition plate shall be attached with fillet welds on each side with a minimum leg of 3/4 t from Paragraph RCB-9.132. Other types of attachments are allowed but shall be of equivalent strength.

Special consideration must be given to reinforcement or thickness requirements for internal partitions subjected to pulsating fluids, extreme differential pressures and/or temperatures, undue restraints or detrimental deflections under specified operating conditions or unusual start-up or maintenance conditions specified by the purchaser. Consideration may also be given to special design configurations and/or methods of analysis which may justify reduction of pass partition plate thickness requirements. Also, consideration should be given to potential bypass of tubeside fluid where the pass partition might pull away from the gasket due to deflection.

RCB-9.134 SPECIAL PRECAUTIONS

RCB-9.14 POSTWELD HEAT TREATMENT Fabricated channels and bonnets shall be postweld heat treated when required by the Code or specified by the purchaser.



90

RCB-9.2 FUT-CHANNEL COVER

*RCB-9.21 FLAT CHANNEL COVER DEFLECTION - MULTIPASS UNITS The effective thickness of a flat channel cover shall be the thickness at the bottom of the pass partition groove (or the face if there is no groove) minus corrosion allowance in excess of groove depth, The thickness is to be at least that required by the appropriate Code formula and thicker if required to meet proper deflection criteria. The recommended limit for channel cover deflection is:

0.03" (0.8 mm) for nominal diameters thru 24" (610 mm) 0.1 25% of nominal diameter (nominal diameter/800) for larger sizes

A method for calculation of channel cover deflection is:

G"

E T 3 y = - ( 0 . 0 4 3 5 G 3 P + O.5SBA,h , )

where Y = Channel cover deflection at the center, inches (mm)

G = Gasket load reaction diameter as defined by the Code, inches (mm)

E = Modulus of elasticity at design temperature, psi (kPa)

T = Thickness under consideration, inches (mm)

P = Design pressure, psi (kPa)

S , = Allowable bolting stress at design temperature, psi (kPa)

A , = Actual total cross-sectional root area of bolts, square inches (mm2)

h = Radial distance from diameter G to bolt circle, inches (mm)

If the calculated deflection is greater than the recommended limit, the deflection may be reduced by acceptable methods such as:

Increase channel cover thickness by the cube root of the ratio of calculated deflection to the recommended limit. Use of strong backs. Change type of construction.

Note: For single pass channels, or others in which there is no pass partition gasket seal against the channel cover, no deflection criteria need be considered.

Channel covers shall be provided with approximately 3/16 (4.8 rnm) deep grooves for pass partitions. In clad or applied facings, all surfaces exposed to the fluid, including gasket seating surfaces, shall have at least 1 /8" (3.2 mm) nominal thickness of cladding.

For design pressures over 300 psi (2068 kPa), channel covers shall be provided with approximately 3/16" (4.8 mm) deep grooves for pass partitions, or other suitable means for holding the gasket in place. In clad or applied facings, all surfaces exposed to fluid, including gasket seating surfaces, shall have at least 1 /8" (3.2mm) nominal thickness of cladding.

R-9.22 CHANNEL COVER PASS PARTITION GROOVES

CB-9.22 CHANNEL COVER PASS PARTITION GROOVES

Stan da r dsOf The TubuwExcha nger-M-uscturers Association


RCB-10 NOZZLES

RCB-10.1 NOZZLE CONSTRUCTION Nozzle construction shall be in accordance with Code requirements. Shell nozzles shall not protrude beyond the inside contour of the shell if they interfere with bundle insertion or removal. Shell or channel nozzles which protrude beyond the inside contour of the main cylinder wall must be self venting or draining by notching at their intersection with the high or low point of the cylinder. If separate vent and drain connections are used, they shall be flush with the inside contour of the shell or channel wall. Flange dimensions and facing shall comply with ASME B16.5. Bolt holes shall straddle natural center lines. Flanges outside the scope of ASME B16.5 shall be in accordance with Code.

RCB-10.2 NOtLLE INSTALLATION Radial nozzles shall be considered as standard. Other types of nozzles may be used, by agreement between manufacturer and purchaser.

R-10.3 PIPE TAP CONNECTIONS All pipe tap connections shall be a minimum of 6000 psi standard couplings or equivalent. Each connection shall be fitted with a round head bar stock plug conforming to ASME B16.11 of the same material as the connection. Alternate plug materiais may be used when galling is anticipated, except cast iron plugs shall not be used.

C-10.3 PIPE TAP CONNECTIONS All pipe tap connections shall be a minimum of 3000 psi standard couplings or equivalent.

8-10.3 PIPE TAP CONNECTIONS All pipe tap connections shall be a minimum of 3000 psi standard couplings or equivalent. Each connection shall be fitted with a bar stock plug of the same material as the connection. Alternate plug materials may be used when galling is anticipated, except cast iron plugs shall not be used.

RCB-10.31 VENT AND DRAIN CONNECTIONS All high and low points on shell and tube sides of an exchanger not otherwise vented or drained by nozzles shall be provided with 3/4" minimum NPS connections for vent and drain.

0 R-10.32 PRESSURE GAGE CONNECTIONS

All flanged nozzles 2" NPS or larger shall be provided with one connection of 3/4" minimum NPS for a pressure gage unless special considerations allow it to be omitted. See Paragraph RB-10.4.

C-10.32 PRESSURE GAGE CONNECTIONS Pressure gage connections shall be as specified by the purchaser. See Paragraph C-10.4.

8-10.32 PRESSURE GAGE CONNECTIONS All flanged nozzles 2" NPS or larger shall be provided with one connection of 1 2" minimum NPS for a pressure gage unless special considerations allow it to be omitted. L ee Paragraph RB-10.4.

RB-10.33 THERMOMETER CONNECTIONS All flanged nozzles 4" NPS or larger shall be provided with one connection of 1" minimum NPS for a thermometer unless special considerations allow it to be omitted. See Paragraph RB-10.4.

C-10.33 THERMOMETER CONNECTIONS Thermometer connections shall be as specified by the purchaser. See Paragraph C-10.4.

RB-10.4 STACKED UNITS Intermediate nozzles between units shall have flat or raised face flanges. Pressure gage and thermometer connections may be omitted in one of the two mating connections of units connected in series. Bolting in flanges of mating connections between stacked exchangers shall be removable without moving the exchangers.



C-10.4 STACKED UNITS Intermediate nozzles between units shall have flat or raised face flanges. Pressure gage and thermometer connections may be omitted in one of the two mating connections of units connected in series.

RCB-10.5 SPLIT FLANGE DESIGN Circumstances of fabrication, installation, or maintenance may preclude the use of the normal integral or loose full ring nozzle flanges. Under these conditions, double split ring flanges may be used in accordance with the Code.

*RCB-10.6 NOZLES LOADINGS Heat exchangers are not intended to serve as anchor points for piping; therefore, for purposes of design, nozzle loads are assumed to be negligible, unless the purchaser specifically details such loads in his inquiry as indicated in Figure RGP-RCB-10.6. The analysis and any modifications in the design or construction of the exchanger to cope with these loads shall be to the purchaser's account. The "Recommended Good Practice" section of these standards provides the designer with additional information regarding imposed piping loads.


MECHANICAL STANDARDS TEMA CLASS R c B SECTION 5

RCB-11 END FLANGES AND BOLTING Flanges and bolting for external joints shall be in accordance with Code design rules, subject to the limitations set forth in the following paragraphs.

R-11.1 MINIMUM BOLT SIZE The minimum permissible bolt diameter is 3/4" M20). Sizes 1" and smaller shall be Coarse Thread Series, and larger sizes shall be 8-Pitch Thread 6 eries. Dimensional standards are included in Section 9, Table D-5. Metric thread pitch is shown in Section 9, Table D-5M.

C-11.1 MINIMUM BOLT SIZE The minimum recommended bolt diameter is 1/2" (M14). If bolting smaller than 1 /2" (M14) is used, precautions shall be taken to avoid overstressing the bolting. Dimensional standards are included in Section 9, Table 0-5. Metric bolting is shown in Section 9, Table D-5M.

B-11.1 MINIMUM BOLT SIZE The minimum permissible bolt diameter shall be 5 / 8 (M16). Dimensional standards are included in Section 9, Table D-5. Metric bolting is shown in Section 9, Table D-5M.

RCB-11.2 BOLT CIRCLE LAYOUT

RCB-11.21 MINIMUM RECOMMENDED BOLT SPACING The minimum recommended spacing between bolt centers is given in Section 9, Table D-5 or D-5M.

RCB-11.22 MAXIMUM RECOMMENDED BOLT SPACING The maximum recornmended spacing between bolt centers is:

6t ( m + 0.5) B m a X = 2 d 6 +

where B = Bolt spacing, centerline to centerline, inches (mm)

d = Nominal bolt diameter, inches (mm)

1 = Flange thickness, inches (mm)

rn = Gasket factor used in Code flange calculations

RCB-11.23 LOAD CONCENTRATION FACTOR When the distance between bolt centerlines exceeds recornmended B ,axI the total flange moment determined by Code design methods shall be multiplied by a correction factor equal to:

where B is the actual bolt spacing as defined by Paragraph RCB-11.22.

RCB-11.24 BOLT ORIENTATION Bolts shall be evenly spaced and normally shall straddle both natural centerlines of the exchanger. For horizontal units, the natural centerlines shall be considered to be the horizontal and vertical centerlines of the exchanger. In special cases, the bolt count may be changed from a multiple of four.

Minimum recommended wrench and nut clearances are given in Section 9, Table D-5 and Table D6M.

RCB-11.3 MINIMUM RECOMMENDED WRENCH AND NUT CLEARANCES



RCB-11.4 BOLT TYPE Except for special design considerations, flanges shall be through-bolted with stud bolts, threaded full length with a removable nut on each end. One full stud thread shall extend beyond each nut to indicate full engagement.

See "Recommended Good Practice" section. *RCB-11.5 LARGE DIAMETER LOW PRESSURE FLANGES

*RCB-11.6 BOLTING-ASSEMBLY AND MAINTENANCE See "Recommended Good Practice" section.


FLOW INDUCED VIBRATION SECTION 6

(Note: This section is not metricated.)

V-1 SCOPE AND GENERAL

V-1.1 SCOPE Fluid flow, inter-related with heat exchanger geometry, can cause heat exchanger tubes to vibrate. This phenomenon is highly complex and the present state-of-the-art is such that the solution to this problem is difficult to define. This section defines the basic data which should be considered when evaluating potential flow induced vibration problems associated with heat exchangers. When potential flow induced vibration problems are requested to be evaluated, the relationships presented in this section and/or other methods may be used. Due to the complexity of the problem, the TEMA guarantee does not cover vibration damage.

V-1.2 GENERAL Damaging tube vibration can occur under certain conditions of shell side flow relative to baffle configuration and unsupported tube span. The maximum unsupported tube spans in Table RCB-4.52 do not consider potential flow induced vibration problems. In those cases, where the analysis indicates the probability of destructive vibration, the user should refer to Paragraph V-13.

V-2 VIBRATION DAMAGE PATFERNS Mechanical failure of tubes resulting from flow induced vibration may occur in various forms. Damage can result from any of the following independent conditions, or combinations thereof.

V-2.1 COLLISION DAMAGE Impact of the tubes against each other or against the vessel wall, due to large amplitudes of the vibrating tube, can result in failure. The impacted area of the tube develops the characteristic, flattened, boat shape spot, generally at the mid-span of the unsupported length. The tube wall eventually wears thin, causing failure.

Baffle tube holes require a manufacturing clearance (see Paragraph RCB-4.2) over the tube outer diameter to facilitate fabrication. When large fluid forces are present, the tube can impact the baffle hole causing thinning of the tube wall in a circumferential, uneven manner, usually the width of the baffle thickness. Continuous thinning over a period of time results in tube failure.

Tubes may be expanded into the tubesheet to minimize the crevice between the outer tube wall and the tubesheet hole. The natural frequency of the tube span adjacent to the tubesheet is increased by the clamping effect. However, the stresses due to any lateral deflection of the tube are also maximum at the location where the tube emerges from the tubesheet, contributing to possible tube breakage.

Designs which were determined to be free of harmful vibrations will contain tubes that vibrate with very small amplitude due to the baffle tube hole clearances and the flexibility of the tube span. Such low level stress fluctuations are harmless in homogeneous material. Flaws contained within the material and strategically oriented with respect to the stress field, can readily propagate and actuate tube failure. Corrosion and erosion can add to such failure mechanisms.

V-2.2 BAFFLE DAMAGE

V-2.3 TUBESHEET CLAMPING EFFECT

V-2.4 MATERIAL DEFECT PROPAGATION

V-2.5 ACOUSTIC VIBRATION Acoustic resonance is due to gas column oscillation and is excited by phased vortex shedding. The oscillation creates an acoustic vibration of a standing wave type. The generated sound wave will not affect the tube bundle unless the acoustic resonant frequency approaches the tube natural frequency, althou h the heat exchanger shell and the attached piping may vibrate, accompanied with loud noise. ahen the acoustic resonant frequency approaches the tube natural frequency, any tendency toward tube vibration will be accentuated with possible tube failure.

V-3 FAILURE REGIONS Tube failures have been reported in nearly all locations within a heat exchanger. Locations dfelatively flexible tube spans and/or high flow velocities are regions of primary concern.


SECTION 6 FLOW INDUCED VIBRATION

V-3.1 U-BENDS Outer rows of U-bends have a lower natural frequency of vibration and, therefore, are more susceptible to flow induced vibration failures than the inner rows.

Impingement plates, large outer tube limits and small nozzle diameters can contribute to restricted entrance and exit areas. These restricted areas usually create high local velocities which can result in producing damaging flow induced vibration.

V-3.2 NOZZLE ENTRANCE AND EXIT AREA

V-3.3 TUBESHEET REGION Unsupported tube spans adjacent to the tubesheet are frequently longer than those in the baffled region of the heat exchanger, and result in lower natural frequencies. Entrance and exit areas are common to this region. The possible high local velocities, in conjunction with the lower natural frequency, make this a region of primary concern in preventing damaging vibrations.

V-3.4 BAFFLE REGION Tubes located in baffle windows have unsupported spans equal to multiples of the baffle spacing. Long unsupported tube spans result in reduced natural frequency of vibration and have a greater tendency to vibrate.

Any obstruction to flow such as tie rods, sealing strips and impingement plates may cause high localized velocities which can initiate vibration in the immediate vicinity of the obstruction.

V-3.5 OBSTRUCTIONS

V-4 DIMENSIONLESS NUMBERS

V-4.1 STROUHAL NUMBER Shedding of vortices from isolated tubes in a fluid medium is correlated by the Strouhal Number, which is given by:

where

f = Vortex shedding frequency, cycles/sec

I/ =

d o =

Crossflow velocity of the fluid relative to the tube, ft/sec

Outside diameter of tube, inches

For integrally finned tubes:

d o = Fin root diameter, inches

Note: In closely spaced tube arrays, the rhythmic shedding of vortices degenerates into a broad turbulence and a correlation based on Strouhal Number alone is inadequate.

V-4.2 FLUID ELASTIC PARAMETER A dimensionless parameter used in the correlations to predict flow induced vibration is given by:

144woST X = 2 P o d o



where w 0 = Effective weight of the tube per unit length, defined in Paragraph V-7.1, Ib/ft

6 = Logarithmic decrement in the tube unsupported span (see Paragraph V-8)

p = Density of the shell side fluid at its local bulk temperature, lb/ft

d o = Outside diameter of tube, inches


d o = Fin root diameter, inches

V-5 NATURAL FREQUENCY

V-5.1 GENERAL Most heat exchangers have multiple baffle supports and varied individual unsupported spans. Calculation of the natural frequency of the heat exchanger tube is an essential step in estimating its potential for flow induced vibration failure. The current state-of-the-art flow induced vibration correlations are not sophisticated enough to warrant treating the rnulti-span tube vibration problem (or mode shapes other than the fundamental) in one comprehensive analysis. Therefore, the potential for vibration is evaluated for each individual unsupported span, with the velocity and natural frequency considered being that of the unsupported span under examination. For more complex mode shapes and multi-spans of unequal lengths, see Paragraph V-14 Reference (10).

The individual unsupported span natural frequency is affected by: V-5.2 FACTORS AFFECTING NATURAL FREQUENCY

(1) Tube elastic and inertial properties and tube geometry. (2) Span shape. (3) Type of support at each end of the unsupported span. (4) Axial loading on the tube unsupported span. (see Paragraph V-6)

V-5.21 SPAN SHAPES The basic span shapes are the straight span and the U-bend span.

The common support conditions are: V-5.22 SPAN SUPPORTS

(1) Fixed at the tubesheet and simply supported at the baffle. (2) Simply supported at each baffle.

The baffle supports have clearances which render them non-linear when analyzed as a support. The tubesheet is not rigid and, therefore, the "built-in" assumption is only approximate. These approximations are known to have minor effects on the calculated natural frequency.

V-5.3 FUNDAMENTAL NATURAL FREQUENCY CALCULATION The value of the fundamental natural frequency of a tube unsupported span can be calculated for the combinations of span shape and end support conditions using Table V-5.3

where f = Fundamental natural frequency of the tube unsupported span, cycles/sec

1 = Tube unsupported span as shown in Table V-5.3, inches

E = Elastic modulus of tube material at the tube metal temperature, psi (see Paragraph RCB-1.43)

w 0 = Effective weight of the tube per unit length, defined in Paragraph V-7.1, Ib/ft


FLOW INDUCE

4 I = Moment of inertia of the tube cross section, inches is given by:

n 64

I = - ( d o '-d, ')

d I = Tube inside diameter, inches


For integrally finned tubes: d = Fin root diameter, inches



r .

TABLE V-5.3 FUNDAMENTAL NATURAL FREQUENCY

Span Geometry

1

2

SDan Geometw

C

9.9

15.42

Edne condition: both ends fixed

(4)

Edge condition: both ends simply supported



(7)


Equation

"1 1 / 2

W Q

Nomenclature

I = Tube axial stress multiplier. See Paragraph V-6

I = Constant depending on edge condition geometry.

r = Mean bend radius, inches

c , = Mode constant of U-bend

Span Geometry C u Figure

v-5.3

V-5.3.1

V-5.3.2

V-5.3.3



Lo 0 (u ru 0 0

100

Ln rl

0

FIGURE V-5.3 U-BEND MODE CONSTANT, C

0

[D

0

m

0

'p

0 m

0

(u

0 rl

0

0

0

0 0

Lo 0

0 0

n

1 \

3



FIGURE V-5.3.1

U U-BEND MODE CONSTANT, C

0

0 0 In Lo (u N

0 0 0 0

d d

3 0

In 0 0 0

0 0



FIGURE V-5.3.2 U-BEND MODE CONSTANT, C

0 aD 0

0 u)

0

0 v 0

0 N

0

0 0

0

0

u)

0

In

n

L \ o n

0

0 0

. .

1 02 Standards Of The Tubular Exchanger Manufacturers Association

FIGURE V-5.3.3 U-BEND MODE CONSTANT, C

I

I

0 0 0 m Lo w 0 0 0

3 u

0 N

0

0 0

0


SECTION 6 FLOW' INDUCED VIBRATION

V-6 AXIAL TUBE STRESS

V-6.1 AXIAL TUBE STRESS MULTIPLIER By the very function of a heat exchanger, the tubes are subjected to axial loads. Compressive axial loads decrease the tube natural frequency, and tensile loads tend to increase it. The resulting tube axial stress multiplier for a given tube unsupported span is determined by the tube end support conditions.

F

where

F = S , A ,

s = Tube longitudinal stress, psi (for fixed tubesheet exchanger, .? may be calculated from Paragraph RCB-7.23)

2 A = Tube metal cross sectional area, inches (see Table D-7)

K 2 E I l 2

F c R = -

K = J l for both ends simply supported

K =I 4.49 for one end fixed, other end simply supported

K = 2 J l for both ends fixed

E = Elastic modulus of tube material at the tube metal temperature, psi (see Paragraph RCB-1.43)

1 = Tube unsupported span, inches

I = Moment of inertia of the tube cross-section, inches (see Paragraph V-5.3 and Table D-7)

4

V-6.2 U-TUBES For some applications U-tubes may develop high levels of axial stress. A method to compute the tube axial stresses in the legs of U-tube exchangers is given in Paragraph V-14, Reference (1).

V-7 EFFECTIVE TUBE MASS To simplify the application of the formulae, the constants have been modified to enable the use of weight instead of mass.

V-7.1 EFFECTIVE TUBE WEIGHT Effective tube weight is defined as:

w o = w , + wf,+ H ,

where

UI = Total metal weight per unit length of tube, Ib/ft (see Table 0-7)

W f = 0.00545 p id

H m = Hydrodynamic mass from Paragraph V-7.11

I= Weight of fluid inside the tube per unit length of tube, Ib/ft



where

p =

d = Inside diameter of tube, inches

Density of fluid inside the tube at the local tube side fluid bulk temperature, Ib/ft

V-7.11 HYDRODYNAMIC MASS Hydrodynamic mass is an effect which increases the apparent weight of the vibrating body due to the displacement of the shell side fluid resulting from:

(1) Motion of the vibrating tube (2) The proximity of other tubes within the bundle (3) The relative location of the shell wall

Hydrodynamic mass is defined as:

Hrn = CrnWf*

where

c W ~ O = 0.00545 p d where

= Added mass coefficient from Figure V-7.11

= Weight of fluid displaced by the tube per unit length of tube, Ib/ft

p = Density of fluid outside the tube at the local shell side fluid bulk temperature,

Ib/ft3 (For two phase fluids, use two phase density.)



d = Fin root diameter, inches


SECTION 6 FLOW INDUCED VIBRAT

FIGURE V-7.11

TUBE PITCH

TUBE OD



V-8 DAMPING

SECTION 6

The mechanisms involved in damping are numerous, and the various effects are not readily measured or quantified. The following expressions for logarithmic decrement, 6 observations and idealized models.

are based strictly on experimental

For shell side liquids, 6 .is equal to the greater of 6 or 6 .

3.41 do 6 , =

W O f n

where p = Shell side liquid viscosity, at the local shell side liquid bulk temperature, centipoise d = Outside diameter of tube, inches. For integrally finned tubes,

do = Fin root diameter, inches

p = Density of shell side fluid at the local bulk temperature, Ib/ft

f = Fundamental natural frequency of the tube span, cycles/sec ui = Effective weight of the tube as defined in Paragraph V-7.1, Ib/ft

For shell side vapors 6 = 6 as follows: 1

6, = 0.314- N where

N = Number of spans t = Baffle or support plate thickness, inches

1 =Tube unsupported span, inches

For two phase shell side media

where f ( E ) = Void fraction function

= I for 0.4 F E, 50 .7 E,- 0.7

= 1 --( o,3 ) for E9.>o.7

c/ , = Voiume flowrate of gas, ft 3/sec

I/ I = Volume flowrate of liquid, ft 3/sec

f ( s , ) = Surface tension function

S T

s 7-70 - - -


SECTION 6

1.20 1.25 1.33 1.50

FLOW INDUClED VlBRATlON

2.25 1.87 2.03 1.72 1.78 1.56 1.47 1.35

S , = Surface tension of shell side liquid at the local bulk temperature. (See Paragraph V-14, Reference (20))

s = Surface tension of shell side liquid at ambient temperature. (See Paragraph

P = Density of shell side liquid at the local bulk temperature, Ib/ft

P = Density of shell side gas at the local bulk temperature, Ib/ft

d o = Outside diameter of tube, inches. For integrally finned tubes, d o = Fin root

W , = Effective tube weight as defined in Paragraph V-7.1, Ib/ft

V-14, Reference (20))

diameter, inches

Note: Use two phase density in the calculation for hydrodynamic mass

P 7 p = Two phase density at local bulk temperature Ib/ft

= P ( ( 1 - E g ) + P , E g

c FU = Confinement function, see Table V-8

Total two phase damping

6, = 6,, + 6, +. 6,

Note: Use two phase properties for density and hydrodynamic mass.

TABLE V-8 CONFINEMENT FUNCTION

c FLI

Tube Pitch Tube OD

Triangular Pitch c F"

Square Pitch CF"


FLOW INDUCE RATt s

V-9 SHELL SIDE VELOCITY DISTRIBUTION

V-9.1 GENERAL One of the most important and least predictable parameters of flow induced vibration is fluid velocity. To calculate the local fluid velocity at a particular point in the heat exchanger is a difficult task. Very complex flow patterns are present in a heat exchanger shell. Various amounts of fluid bypass the tube bundle or leak through clearances between baffles and shell, or tube and baffle tube holes. Until methods are developed to accurately calculate local fluid velocities, the designer may use average crossflow velocities based on available empirical methods.

V-9.2 REFERENCE CROSSFLOW VELOClTY The crossflow velocity in the bundle varies from span to span, from row to row within a span, and from tube to tube within a row. The reference crossflow velocity is calculated for each region of interest (see Paragraph V-3) and is based on the average velocity across a representative tube row in that region. The presence of pass partition lanes aligned in the crossflow direction, clearance between the bundle and the shell, tube-to-baffle hole annular clearances, etc. reduce the net flow rate of the shell side fluid in crossflow. This should be considered in computing the reference crossflow velocity.

V-9.21 REFERENCE CROSSFLOW VELOCITY CALCULATIONS The following method of calculating a reference crossflow velocity takes into account fluid bypass and leakage which are related to heat exchanger geometry. The method is valid for single phase shell side fluid with single segmental baffles in TEMA E shells. Other methods may be used to evaluate reference crossflow velocities. Reference crossflow velocity is given by:

V-9.211 CALCULATION OF CONSTANTS The constants used in the calculation of the reference crossflow velocity are given by:

DI c , = - D3

d , - d 0 c, = - d0

c, = 0.00674( T) P - d ,


ION 6

c4

c5

C6

m

110

TUBE PATTERN (See Figure RCB-2.4)

30" 60" 90" 45"

1.26 1.09 1.26 0.90

0.82 0.61 0.66 0.56

1.48 1.28 1.38 1.17

0.85 0.87 0.93 0.80

TABLE V-9.211A

h D1 _.

C8

0.10 0.15 0.20 0.25 0.30 0.35 0.40 0.45 0.50

0.94 0.90 0.85 0.80 0.74 0.68 0.62 0.54 0.49

TABLE V-9.211 B

h C 8 vs cut-toiiiameter ratio

Linear interpolation is permitted

M,= ( r n ) ( C , ) " *

r 1

a, = (13)(D3)(Ca)

where D = Shell inside diameter, inches

D 2 = Baffle diameter, inches

D = Outer tube limit (OTL), inches

d I = Tube hole diameter in baffle, inches


s 6


For integrally finned tubes: d o = Fin outside diameter, inches

P = Tube pitch, inches

1 = Baffle spacing, inches

P o = Density of shell side fluid at the local bulk temperature, Ib/ft

W = Shell fluid flow rate, Ib/hr

h = Height from baffle cut to shell inside diameter, inches

V-9.3 SEAL STRIPS Seal strips are often used to help block the circumferential bypass space between a tube bundle and shell, or other bypass lanes. Seal strips force fluid from the bypass stream back into the bundle. This increases the reference crossflow velocity and should be considered in a vibration analysis. Local fluid velocity in the vicinity of seal strips may be significantly higher than the average crossflow velocity. (See Paragraph V-14, Reference 6.)

V-9.31 REFERENCE CROSSFLOW VELOCITY WITH SEAL STRIPS

The reference crossflow velocity is calculated by using a modified value for c in the equations in Paragraph V-9.211.

L 4 J

V-9.4 PASS LANES PARALLEL TO FLOW When pass lanes are oriented parallel to flow (at 90" to the baffle cut) they create a relatively low resistance path for fluid to follow. The net effect is for less fluid to cross the tube bundle, resulting in a lower average crossflow velocity. However, tubes adjacent to these lanes may be subjected to high local velocities. The number and width of these lanes should be considered when the reference crossflow velocity is calculated.

V-9.41 REFERENCE CROSSFLOW VELOCITY WITH PASS LANES PARALLEL TO FLOW To account for pass lanes arallel to flow, if they are not blocked by some type of special

where

baffle, a modified value of f3 can be used

D = Outer tube limit minus (number of parallel pass lanes x width of pass lanes), inches

V-9.5 BUNDLE ENTRANCE REGION AND IMPINGEMENT PLATES Tubes directly beneath inlet nozzles and impingement plates can be subjected to local fluid velocities greater than those in other parts of the bundle. A number of documented vibration problems have been caused by high inlet fluid velocities. These standards provide guidedines for maximum velocity in this region and set criteria for the use of impingement plates. The p If limits in Paragraph RCB-4.6 are furnished for protection against tube erosion, but do not necessarily prevent vibration damage.

In computing the reference crossflow velocity, the presence of fins shall be taken into account. For the purposes of using the equations in Paragraph V-9.2 to calculate a reference crossflow velocity, the fin diameter should be used in place of the nominal tube OD for integrally finned tubes.

V-9.6 INTEGRALLY FINNED TUBES

__



V-10 ESTIMATE OF CRITICAL FLOW VELOCITY

The critical flow velocity, I/ , for a tube span is the minimum cross-flow velocity at which that span may vibrate with unacceptably large amplitudes. The critical flow velocity for tube spans in the window, overlap, inlet and outlet regions, U-bends, and all atypical locations should be calculated. The critical velocity, V , is defined by:

where D =

f = Fundamental natural frequency, cycles/sec (see Paragraph V-5.3)

d o = Outside diameter of tube, inches For integrally finned tubes: d o =

Value obtained from Table V-10.1

Fin root diameter, inches

The user should ensure that the reference crossflow velocity V, at every location, is less than 1’- for that location.



TABLE V-1 0.1 FORMULAE FOR CRITICAL FLOW VELOCITY FACTOR, D

over 1 to 300

0.03 to 0.7

over 0.7 to 300

Tube Pattern (See Figure RCB-2.4)

2.80 x O.'

2. lox'

2 . 3 5 ~ ~ '

30'

60 '

90'

45 O

Parameter Range for

X

_ _ ~

Dimensionless Critical Flow Velocity Factor, D

0.1 to 1

over 1 to 300

0.01 to 1 2.80 x ' . I 7

0.1 to300

p = Tube pitch, inches d = Tube OD or fin root diameter for integrally finned tubes, inches

1 4 4 ~ ~ 6 , X = = Fluid elastic parameter

P ,do

where

3 P o = Shell side fluid density at the corresponding local shell side bulk temperature, Ib/ft

6 ,- = Logarithmic decrement (See Paragraph V-8)

w = Effective weight of the tube per unit length, Ib/ft (See Paragraph V-7.1)


V-11 VIBRATION AMPLITUDE V-11.1 GENERAL There are four basic flow induced vibration mechanisms that can occur in a tube bundle. These are the fluidelastic instability, vortex shedding, turbulent buffeting, and acoustic resonance. The first three mechanisms are accompanied by a tube vibration amplitude while acoustic resonance causes a loud acoustic noise with virtually no increase in tube amplitude. Fluidelastic instability is the most damaging in that it results in extremely large amplitudes of vibration with ultimate damage patterns as described in Paragraph V-2. The design approach in this case is to avoid the fluidelastic instability situation thereby avoiding the accompanying large amplitude of vibration (see Paragraph V-10). Vortex shedding may be a problem when there is a frequency match with the natural frequency of the tube. Vibration due to vortex shedding is expected when f < 2 f u s , where f =c 1 2 SV 1 d o (see Paragraph V-12.2). Only then should the amplitude be calculated. This frequency match may result in a vibration amplitude which can be damaging to tubes in the vicinity of the shell inlet and outlet connections. Vortex shedding degenerates into broad band turbulence and both mechanisms are intertwined deep inside the bundle. Vortex shedding and turbulent buffeting vibration amplitudes are tolerable within specified limits. Estimation of amplitude and respective limits are shown below.

V-11.2 VORTEX SHEDDING AMPLITUDE

CLPOdOV2 2 n 2 6 , f f w , Y”, =

where

Y,, =

C , =

P o =

d o =

I/=

6 , =

f n =

W o =

Peak amplitude of vibration at midspan for the first mode, for single phase fluids, inches Lii coefficient for vortex shedding, (see Table V-11.2)

Density of fluid outside the tube at the local shell side fluid bulk temperature, Ib/it3

Outside diameter of tube, inches For integrally finned tubes, d =fin root diameter, inches

Reference crossflow velocity, ft/sec (see Paragraph V-9.2)

Logarithmic decrement (see Paragraph V-8)

Fundamental natural frequency of the tube span, cycles/sec (see Paragraph V-5.3)

Effective tube weight per unit length of tube, lb/ft (see Paragraph V-7.1)

V-11.21 RECOMMENDED MAXIMUM AMPLITUDE y,, 5 0.02d0 , inches

V-1 1.3 TURBULENT BUFFETING AMPLITUDE

C F P o d o V 2 Y t B = an6, i/2f 3 / Z w 0

where y L B = Maximum amplitude of vibration for single phase fluids, inches

C = Force coefficient (see Table V-1 1.3)

V-11.31 RECOMMENDED MAXIMUM AMPLITUDE y t B 5 0.02d0 , inches


FLOW IND

P d o

1.20 1.25 1.33 1.50

-

SECT[

TUBE PATTERN (See Figure RCB-2.4)

30" 60" 90" 45"

0.090 0.090 0.070 0.070 0.091 0.091 0.070 0.070 0.065 0.01 7 0.070 0.010 0.025 0.047 0.068 0.049

TABLE V-11.2

TABLE V-11.3 FORCE COEFFICENTS

CF

Location

Bundle Entrance Tubes

Interior Tubes

~

1

f n

I 4 0

> 4 0 < 8 8 2 88

0.022

-0.00045fa + 0.04 0 I

L 40

> 4 0 < 8 8 2 88

0.012

I -0.00025fn + 0.022 0 I

I

-



V-12 ACOUSTIC VIBRATION

Acoustic resonance is due to a gas column oscillation. Gas column oscillation can be excited by phased vortex shedding or turbulent buffeting. Oscillation normally occurs perpendicular to both the tube axis and flow direction. When the natural acoustic frequency of the shell approaches the exciting frequency of the tubes, a coupling may occur and kinetic energy in the flow stream is converted into acoustic pressure waves. Acoustic resonance may occur independently of mechanical tube vibration. V-12.1 ACOUSTIC FREQUENCY OF SHELL

Acoustic frequency is given by:

116

where UI = Distance between reflecting walls measured parallel to segmental baffle cut, inches

P = Operating shell side pressure, psia

y = Specific heat ratio of shell side gas, dimensionless

P = Shell side fluid density at local fluid bulk temperature, Ib/ft

Pl X I = -

d0

p I = Longitudinal pitch, inches (see Figures V-l2.2A and V-12.28)

p I = Transverse pitch, inches (see Figures V-l2.2A and V-12.28)

d o = Outside diameter of tube, inches. For integrally finned tubes, d o = Fin outer diameter, inches

i = mode (1, 2, 3, 4)

V-12.2 VORTEX SHEDDING FREQUENCY The vortex shedding frequency is given by:

.f u s = - , cycles/sec 12sv

d0

where

I/ = Reference crossflow velocity, ft/sec (see Paragraph V-9.2)

S = Strouhal number (see Figures V-12.2A and V-12.29)



d o = Fin outer diameter, inches



V-12.3 TURBULENT BUFFETING FREQUENCY The turbulent buffeting frequency is given by:

fib= 12' [ 3.05 ( 1 -- if)* +0.28 1 ,cycles/sec d O X l X t

where



d o = Fin outer diameter, inches

Pt x, = - do

p = Longitudinal pitch, inches (see Figures V-12.2A and V-12.2B)

p I = Transverse pitch, inches (see Figures V-l2.2A and V-12.28)

V = Reference crossflow velocity, ft/sec (see Paragraph V-9.2)

V-12.4 ACOUSTIC RESONANCE Incidence of acoustic resonance is possible if any one of the following conditions is satisfied at any operating condition.

V-12.41 CONDITION A PARAMETER

0 * 8 .f u s < f a < 1 -2 f us

or

0.8f tb < f a < *2f l b

V-12.42 CONDITION B PARAMETER

V-12.43 CONDITION C PARAMETER

and

where x = x for 90" tube patterns

x = 2 x for 30", 45", and 60" tube patterns

f a = Acoustic frequency, cycles/sec (see Paragraph V-12.1)

S = Strouhal number (see Figures V-l2.2A and V-12.2B)



R = Reynolds number, evaluated at the reference cross flow velocity

124 .13doV[ /p ,

P R , =

p = Shellside fluid viscosity, centipoise

V-12.5 CORRECTIVE ACTION There are several means available to correct a resonant condition, but most could have some effect on exchanger performance. The simplest method is to install deresonating baffle@) in the exchanger bundle to break the wave(s) at or near the antinode@). This can be done without significantly affecting the shell side flow pattern. In shell and tube exchangers, the standing wave forms are limited to the first or the second mode. Failure to check both modes can result in acoustic resonance, even with deresonating baffles.


0 . 5

0 . 4

0 . 2

S 0.2

O . !

0

RATION

FIGURE V-12.2A STROUHAL NUMBER FOR 90 TUBE PATTERNS

2 3 4

FLOW


s

0.

0.

0.

0.

0.

0.

0.

0.

0.

FIGURE V-12.2B STROUHAL NUMBER FOR 30 O ,4!5 O AND 60 O TUBE PATTERNS

5

2. Pr

do

FLOW

625 /do = 3.95



V-13 DESIGN &ONSIDERATIONS Many parameters acting independently or in conjunction with each other can affect the flow induced vibration analysis. One must be cognizant of these parameters and their effects should be accounted for in the overall heat exchanger design.

V-13.1 TUBE DIAMETER Use of the largest reasonable tube diameter consistent with practical thermal and hydraulic design economics is desirable. Larger diameters increase the moment of inertia, thereby effectively increasing the stiffness of the tube for a given length.

The unsupported tube span is the most significant factor affecting induced vibrations. The shorter the tube span, the greater its resistance to vibration. The thermal and hydraulic design of an exchanger is significant in determining the type of shell, baffle design and the unsupported tube length. For example, compared to single pass shells, a divided flow shell will result in approximately one-half the span length for an equal crossflow velocity. TEMA type X shells provide the opportunity to use multiple support plates to reduce the unsupported tube span, without appreciably affecting the crossflow velocity. Com red to the conventional segmental baffle flow arrangement, multi-segmental baffles

drop. "No tubes in window" flow arrangement baffles provide support to all tubes at all baffle locations and also permit the use of multiple intermediate supports without affecting the crossflow velocity while reducing the unsupported tube span.

Larger pitch-to-tube diameter ratios provide increased ligament areas which result in a reduced crossflow velocity for a given unsupported tube span, or a reduced unsupported tube span for a given crossflow velocity. The increased tube to tube spacing reduces the likelihood of mid-span collision damage and also decreases the hydrodynamic mass coefficient given in Figure V-7.11.

Entrance and exit areas are generally recognized to be particularly susceptible to damage in vibration prone exchangers. Entrance and exit velocities should be calculated and compared to critical velocities to avoid vibration of the spans in question. It should be noted that compliance with Paragraph RCB4.62 alone is not enough to insure protection from flow induced vibration at the entrance/exit regions of the bundle. Consideration may be given to the use of partial supports to reduce unsupported tube spans in the entrance/exit regions. Sufficient untubed space may have to be provided at the shell inlet/outlet connections to reduce entrance/exit velocities. Impingement plates should be sized and positioned so as not to overly restrict the area available for flow. The use of distribution belts can be an effective means of lowering entrance/exit velocities by allowing the shell side fluid to enter/exit the bundle at several locations.

Susceptibility of U-bends to damaging vibration may be reduced by optimum location of adjacent baffles in the straight tube legs and/or use of a s ecial bend support device.

appropriately locating the shell connection and/or adjacent baffles.

The natural frequency of an unsupported tube span is affected by the elastic modulus of the tube. High values of elastic moduli inherent in ferriiic steels and austenitic stainless alloys provide greater resistance to vibratory flexing than materials such as aluminum and brass with relatively low elastic moduli. Tube metallurgy and wall thickness also affect the damping characteristic of the tube.

V-13.2 UNSUPPORTED TUBE SPAN

sign' x" icantly reduce the tube unsupported span for the Same shell side flow rate and pressure

V-13.3 TUBE PITCH

V-13.4 ENTRANCE/EXIT AREAS

V-13.5 U-BEND REGIONS

Consideration may also be given to protecting the bends P rom flow induced vibration by

V-13.6 TUBING MATERIAL AND THICKNESS



122

V-13.7 BAFFLE THICKNESS AND TUBE HOLE SIZE Increasing the baffle thickness and reducing the tube-to-baffle hole clearance increases the system damping (see Paragraph V-8) and reduces the magnitude of the forces acting on the tube-to-baffle hole interface. The formulae in this section do not quantitatively account for the effects of increasing the baffle thickness, or tightening of the baffle hole clearance.

V-13.8 OMISSION OF TUBES Omission of tubes at predetermined critical locations within the bundle may be employed to reduce vibration potential. For instance, tubes located on baffle cut lines sometimes experience excessive damage in vibration prone units; therefore, selective removal of tubes along baffle cut lines may be advantageous.

V-13.9 TUBE AXIAL LOADING The heat exchanger designer must recognize the potential adverse impact on vibration by compressive axial loading of tubes due to pressure and/or temperature conditions. This is particularly significant for tubes in single pass, fixed tubesheet exchangers where the hot fluid is in the tube side, and in all multiple tube pass fixed tubesheet exchangers. The use of an expansion joint in such cases may result in reduction of the tube compressive stress. (See Paragraph V-6.)

V-14 SELECTED REFERENCES (1) Singh, K. P., and Soler, A. I., "Mechanical Design Of Heat Exchangers And Pressure Vessel

(2) Paidoussis, M. P., "Flow Induced Vibration Of Cylindrical Structures: A Review Of The

(3) Barrington, E. A., "Experience With Acoustic Vibrations In Tubular Exchangers", Chemical

(4) Barrington, E. A., "Cure Exchanger Acoustic Vibration", Hydrocarbon Processing, (July, 1978) (5) Chen, S. S., and Chung, Ho, "Design Guide For Calculating Hydrodynamic Mass, Part 1: Circular

Components", Arcturus Publishers, Cherry Hill, N.J., (1984)

State-Of-The-Art", McGill University, Merl Report No. 82-1 (1 982)

Engineering Progress, Vol. 69, No. 7 (1973)

Cylindrical Structures", Argonne National Laboratory, Report No. ANL-CT-76-45 Chung, H., and Chen, S. S., "Design Guide For Calculatin Hydrodynamic Mass, Part II: Noncircular Cylindrical Structures", I bid, Report No. ANL- 8 T-78-49

(6) Kissel, J. H., "Flow Induced Vibration In A Heat Exchanger With Seal Strips", ASME HTD, Vol. 9

(7) Chen, S. S., "Flow Induced Vibration Of Circular Cylindrical Structures", Argonne National

(8) Tinker, T., "General Discussion Of Heat Transfer", Institution Of Mechanical Engineers, pp

(9) Gorman, Daniel J., "Free Vibration Analysis Of Beams & Shafts", John Wiley & Sons, (1 975) (10) Pettigrew, M.J., Goyder, H.G.D., Qiao, Z. L., Axisa, F., "Damping of Multispan Heat Exchanger

Tubes", Part 1: In Gases, Flow-Induced Vibration (1986), ASME PVP Vol. 104, (1986), pp 81 -87 (1 1) Pettigrew, M.J., Taylor, C. E., Kim, B.S., "Vibration of Tube Bundles In Two-Phase Cross Flow:

Part I - Hydrodynamic Mass and Damping", 1988 International Symposium on Flow4 nduced Vibration and Noise - Volume 2, The Pressure Vessel and Piping Division - ASME, pp 79-1 03

(12) Connors, H.J., "Fluidelastic Vibration Of Tube Arrays Excited By Crossflow", Flow Induced Vibration In Heat Exchangers, ASME, New York (1970)

(13) Chen, S.S., "Design Guide For Calculating The Instability Flow Velocity Of Tube Arrays In Crossflow", Argonne National Laboratory, ANL-CT-81-40 (1 981)

(14) Kissel, Joseph H., "Flow Induced Vibrations In Heat Exchangers - A Practical Look, Presented at the 13th National Heat Transfer Conference, Denver (1 972)

(15) Moretti, P.M., And Lowery, R.L., "Hydrodynamic Inertia Coefficients For A Tube Surrounded By Rigid Tubes", ASME paper No. 75-PVR 47, Second National Congress On Pressure Vessel And Piping, San Francisco

(1 980)

Laboratory, Report No. ANL-CT-85-51

97-1 16, London (1 951)

(16) WRC Bulletin 389, dated February 1994


OW INDUCE 6

(1 7) Owen, P.R., "Buffeting Excitation Of Boiler Tube Vibration", Journal Of Mechanical Engineering

(1 8) Byrce, W.B., Wharmsby, J.S. and Fitzpatrick, J., "Duct Acoustic Resonances Induced By Flow Science, Vol. 7, 1965

Over Coiled And Rectangular Heat Exchanger Test Banks Of Plain And Finned Tubes", Proc. BNES International Conference On Vibration In Nuclear Plants, Keswick, U.K. (1 978)

(19) Chen, Y.N., "Flow Induced Vibration And Noise In Tube Bank Heat Exchangers Due To Von Karman Streets," Journal Of Engineering For Industry

(20) API, 'Technical Data Book - Petroleum Refining", 1996


SECTION 7 THERMAL RELATIONS

(Note: This section is not metricated.)

T-1 SCOPE AND BASIC RELATIONS

T-1.1 SCOPE This section outlines the basic thermal relationships common to most tubular heat transfer equipment. Included are calculation procedures for determining mean temperature difference and overall heat transfer coefficient, and discussions of the cause and effect of fouling, and procedures for determining mean metal temperatures of shell and tubes. Recommendations for the calculation of shell side and tube side heat transfer film coefficients and pressure losses are considered to be outside the scope of these Standards. It should be noted, however, that many of the standard details and clearances can significantly affect thermal-hydraulic performance, especially on the shell side. Particularly relevant in this respect is the research conducted by the Universrty of Delaware Engineering Experiment Station under the joint sponsorship of ASME, API, TEMA, and other interested organizations. The results are summarized in their "Bulletin No. 5 (1963) Final Report of the Cooperative Research Program on Shell and Tube Exchangers."

T-1.2 BASIC HEAT TRANSFER RELATION

Q A , = - unt, where

= Required effective outside heat transfer surface, ft*

Q =

U =

At, = Corrected mean temperature difference, O F

Total heat to be transferred, BTU/hr

Overall heat transfer coefficient, referred to tube outside surface BTU/hr ft2 O F

T-1.3 DETERMINATION OF OVERALL HEAT TRANSFER COEFFICIENT The overall heat transfer coefficient U, including fouling, shall be calculated as follows:

1

where U = Overall heat transfer coefficient (fouled)

h, = Film coefficient of shell side fluid

h = Film coefficient of tube side fluid

r = Fouling resistance on outside surface of tubes

r =

r ,,, =

Fouling resistance on inside surface of tubes

Resistance of tube wall referred to outside surface of tube wall, including extended surface if present


THERMAL RELATIONS SECTION 7

,4 0 14 1

- _ - Ratio of outside to inside surface of tubing

E = Fin efficiency (where applicable)

The units of 11, h and h I are BTU/hr ft* O F and the units of r o t r and r =,are hr ft2 O F/BTU

T-1.4 TUBE WALL RESISTANCE

T-1.41 BARE TUBES

T-1.42 INTEGRALLY FINNED TUBES

t [ d + 2 N w ( d + w ) ] r m = ~

1 2 k ( d - t )

where d = OD of bare tube or root diameter if integrally finned, inches

w = Fin height, inches

t = Tube wall thickness, inches

N = Number of fins per inch

k = Thermal conductivity, BTU/hr ft O F

T-1.5 SELECTED REFERENCE BOOKS

(1) A. P. Fraas and M. N. Ozisik, "Heat Exchanger Design", John Wiley & Sons, 1965. (2) M. Jacob, "Heat Transfer", Vol. 1, John Wiley & Sons, 1949. (3) D. Q. Kern, "Process Heat Transfer", McGraw-Hill Book Co., 1950. (4) J. G. Knudsen and D. L. Katz, "Fluid Dynamics and Heat Transfer", McGraw-Hill Book Co., 1958. (5) W. H. McAdams, "Heat Transmission", McGraw-Hill Book Co., Third Ed., 1954. (6) Chemical Engineers' Handbook, McGraw-Hill Book Co., Fifth Ed., 1973.

T-2 FOULING

T-2.1 TYPES OF FOULING Several unique types of fouling mechanisms are currently recognized. They are individually complex, can occur independently or simultaneously, and their rates of development are governed by physical and chemical relationships dependent on operating conditions. The major fouling mechanisms are:

Precipitation fouling Particulate fouling Chemical reaction fouling Corrosion fouling Biological fouling



T-2.2 EFFECTS OF FOULING The calculation of the overall heat transfer coefficient (see Paragraph T-1.3) contains the terms to account for the thermal resistances of the fouling layers on the inside and outside heat transfer surfaces. These fouling layers are known to increase in thickness with time as the heat exchanger is operated. Fouling IayePs normally have a lower thermal conductivity than the fluids or the tube material, thereby increasing the overall thermal resistance. In order that heat exchangers shall have sufficient surface to maintain satisfactory performance in normal operation, with reasonable service time between cleanings, it is important in design to provide a fouling allowance appropriate to the expected operating and maintenance condition.

T-2.3 CONSIDERATIONS IN EVALUATING FOULING RESISTANCE The determination of appropriate fouling resistance values involves both physical and economic factors, many of which vary from user to user, even for identical services. When these factors are known, they can be used to adjust typical base values tabulated in the RGP section of these standards.

T-2.31 PHYSICAL CONSIDERATIONS Typical physical factors influencing the determination of fouling resistances are:

Fluid properties and the propensity for fouling Heat exchanger geometry and orientation Surface and fluid bulk temperatures Local fluid velocities Heat transfer process Fluid treatment Cathodic protection

T-2.32 ECONOMIC CONSIDERATIONS Typical economic factors influencing the determination of appropriate fouling resistances are:

Frequency and amount of cleaning costs Maintenance costs Operating and production costs Longer periods of time on stream Fluid pumping costs Depreciation rates Tax rates Initial cost and variation with size Shut down costs Out-of-service costs

T-2.4 DESIGN FOULING RESISTANCES The best design fouling resistances, chosen with all physical and economic factors properly evaluated, will result in a minimum cost based on fixed charges of the initial investment (which increase with added fouling resistance) and on cleaning and down-time expenses (which decrease with added fouling resistance). By the very nature of the factors involved, the manufacturer is seldom in a position to determine optimum fouling resistances. The user, therefore, on the basis of past experience and current or projected costs, should specify the design fouling resistances for his particular services and operating conditions. In the absence of specific data for setting proper resistances as described in the previous paragraphs, the user may be guided by the values tabulated in the RGP section of these standards. In the case of inside surface fouling, these values must be multiplied by the outside/inside surface ratio, as indicated in Equation T-1.3.

T-3 FLUID TEMPERATURE RELATIONS

T-3.1 LOGARITHMIC MEAN TEMPERATURE DIFFERENCE For cases of true countercurrent or cocurrent flow, the logarithmic mean temperature difference should be used if the following conditions substantially apply:



Constant overall heat transfer coefficient Complete mixing within any shell cross pass or tube pass The number of cross baffles is large Constant flow rate and specific heat Enthalpy is a linear function of temperature Equal surface in each shell pass or tube pass Negligible heat loss to surroundings or internally between passes

The following references contain relevant information on the above items: (1) K. Gardner and J. Taborek, "Mean Temperature Difference - A Reappraisal", AlChE Journal,

(2) A. N. Caglayan and P. Buthod, "Factors Correct Air-Cooler and S & T Exchanger LMTD", The Oil

For cases where the above conditions do not apply, a stepwise calculation of temperature difference and heat transfer surface may be necessary. Excessive fluid leakage through the clearance between the cross baffles and the shell or between a longitudinal baffle and the shell can significantly alter the axial temperature profile. This condition may result in significant degradation of the effective mean temperature difference. The following references may be used for further information on this subject: (1) J. Fisher and R. 0. Parker, "New Ideas on Heat Exchanger Design", Hydrocarbon Processing,

(2) J. W. Palen and J. Taborek, "Solution of Shellside Flow Pressure Drop and Heat Transfer by

December, 1977

& Gas Journal, September 6, 1976

Vol. 48, No. 7, July 1969

Stream Analysis", CEP Symposium No. 92, Vol. 65, 1969

T-3.2 CORRECTION FOR MULTIPASS FLOW In multipass heat exchangers, where there is a combination of cocurrent and countercurrent flow in alternate passes, the mean temperature difference is less than the logarithmic mean calculated for countercurrent flow and greater than that based on cocurrent flow. The correct mean temperature difference may be evaluated as the product of the logarithmic mean for countercurrent flow and an LMTD correction factor, F. Figures T-3.2A to T-3.2M inclusive give values for F as a function of the heat capacity rate ratio R and the required temperature effectiveness P. These charts are based on the assumption that the conditions listed in Paragraph T-3.1 are applicable. Caution should be observed when applying F factors from these charts which lie on the steeply sloped portions of the curves. Such a situation indicates that thermal performance will be extremely sensitive to small changes in operating conditions and that performance prediction may be unreliable. Pass configurations for Figures T-3.2A through T-3.2H are stream symmetric; therefore, t and T may be taken as the cold and hot fluid temperatures, respectively, regardless of passage through the tube side or shell side. For non-stream symmetric configurations represented by Figures T-3.21 through T-3.2M, t and T must be taken as the tube side and the shell side fluid temperatures, respectively. The following references may be useful in determining values of F for various configurations and conditions. Confiauration Reference (1) General W. M. Rohsenow and J. P. Hartnett, "Handbook of Heat

Transfer", McGraw-Hill Book Co., 1972 (2) Three tube passes per shell pass F. K. Fischer, "lnd. Engr. Chem.", Vol. 30,377 (1938) (3) Unequal size tube passes K. A. Gardner, "Ind. Engr. Chem.", Vol. 33, 1215 (1941) (4) Weighted MTD D. L. Gulley, "Hydrocarbon Proc.", Vol. 45, 116 (1966)

T-3.3 TEMPERATURE EFFECTIVENESS The temperature effectiveness of a heat exchanger is customarily defined as the ratio of the temperature change of the tube side stream to the difference between the two fluid inlet temperatures, thus:



( t z - t l )

( T l - t l ) P =

where Pis the effectiveness. Figures T-3.3A, T-3.3B, and T-3.3C show the temperature effectiveness of counterflow, single-pass shell and two-pass tube, and two-pass shell and four-pass tube exchangers respectively, in terms of overall heat transfer coefficient, surface, fluid flow rates, and specific heats.

In all cases, the lower case symbols ( t , t 2 , w a n d c )refer to the tube side fluid, and upper case (T , T z , W a n d C)to the shell side fluid. (This distinction is not necessary in the case of counterflow exchangers, but confusion will be avoided if it is observed.) These charts are based on the same conditions listed in Paragraph T-3.1.

T-4 MEAN METAL TEMPERATURES OF SHELL AND TUBES

T-4.1 SCOPE This paragraph outlines the basic method for determination of mean shell and tube metal temperatures. These temperatures have a pronounced influence in the design of fixed tubesheet exchangers. Knowledge of mean metal temperatures is necessary for determining tubesheet thickness, shell and tube axial stress levels, and flexible shell element requirements. This paragraph provides the basis for determining the differential thermal expansion term, A L , required for the calculation of equivalent differential expansion pressure, P (see Paragraph RCB-7.161).

T-4.2 DEFINITIONS

T-4.21 MEAN METAL TEMPERATURE The mean metal temperature of either the shell or tubes is the temperature taken at the metal thickness midpoint averaged with respect to the exchanger tube length. For the case of integrally finned tubes, the temperature at the prime tube metal thickness midpoint applies. The fin metal temperature should not be weighted with the prime tube metal temperature.

T-4.22 FLUID AVERAGE TEMPERATURE The shell or tube fluid average temperature is the bulk shell or tube fluid temperature averaged with respect to the exchanger tube length.

T-4.3 RELATIONSHIP BETWEEN MEAN METAL TEMPERATURES AND FLUID AVERAGE TEMPERATURES

T-4.31 SHELL MEAN METAL TEMPERATURE The shell mean metal temperature, generally assumed to be equal to the shell fluid average temperature, is given by:

T , = 7

where T , = Shell mean metal temperature, O F

5 = Shell fluid average temperature, F

This assumption is valid for cases without abnormal rates of heat transfer between the shell and its surroundings. If significant heat transfer to or from the shell could occur, determination of the effect on the shell metal temperature should be made. In general, most high or low temperature externally insulated exchangers and moderate temperature non-insulated exchangers meet the above assumption.



T-4.32 TUBE MEAN METAL TEMPERATURE

- t , = T -

The tube mean metal temperature is dependent not only on the tube fluid average temperature, but also the shell fluid average temperature, the shell and tube heat transfer coefficients, shell and tube fouling resistances, and tube metal resistance to heat transfer, according to the following relationship:

-

where t = Tube mean metal temperature, O F

t = Tube side fluid average temperature, O F (see Paragraph T-4.4) -

All other terms are as defined by Paragraphs T-1.3 and T-4.31.

T-4.33 TUBESHEET MEAN METAL TEMPERATURE Untubed portion of tubesheet

T r + T s 2 T r s =

Tubed portion of tubesheet:

where: T = Tubeside fluid temperature, O F T , = Shellside fluid temperature, O F

h j - = Tubeside heat transfer coefficient, BTU/Hr-ftz - O F

h, = Shellside heat transfer coefficient, BTU/Hr-ftZ - O F A

+ - t a n h ( K )

K = J ! ! % a 12k , degrees

where k = tubesheet metal thermal conductivity, BTU/Hr-ft O F

L = tubesheet thickness, inches

1

c o s h ( K ) + y s i n h ( K ) F =



for triangular pitch .4 = n d L / 2

u = 0 . 4 3 3 P 2 - n d 2 / 8

for square pitch A = n d L

a = p 2 - n d 2 / 4

where d = tube ID, inches

p = tube pitch, inches

T-4.4 ESTIMATION OF SHELL AND TUBE FLUID AVERAGE TEMPERATURES The methods presented in this paragraph are based on equipment operating under steady-state conditions.

T-4.41 GENERAL CONSIDERATIONS Fluid average temperatures in shell and tube heat exchangers are affected by the following: (1) Shell and tube fluid terminal temperatures (2) Shell and tube fluid temperature profiles with respect to enthalpy (the following

methods assume linear profiles) (3) Variable heat transfer rates with respect to exchanger length (the following methods

assume a constant heat transfer rate through the length of the unit) (4) Heat exchanger geometry, specifically pass configuration, of the shell as well as the

tubes

T-4.42 ISOTHERMAL SHELL FLUID/ISOTHERMAL TUBE FLUID, ALL PASS ARRANGEMENTS - T = T , = T ,

t = t , = t ,

T , = Shell side fluid inlet temperature, O F T = Shell side fluid outlet temperature, O F t I =Tube side fluid inlet temperature, O F t =Tube side fluid outlet temperature, O F

-

where

T-4.43 ISOTHERMAL SHELL FLUID/LINEAR NONISOTHERMAL TUBE FLUID, ALL PASS ARRANGEMENTS



T-4.44 LINEAR NONISOTHERMAL SHELL FLUID/ISOTHERMAL TUBE FLUID, ALL PASS ARRANGEMENTS

t = t , = t ,

T = i;t L M T D __

T-4.45 LINEAR NONISOTHERMAL SHELL AND TUBE FLUIDS, TYPE "E" SHELL The average shell fluid temperature may be determined from the following equation:

The value of adepends on tube pass geometry and flow direction as given below:

Single pass tubes - cocurrent flow

Single pass tubes - countercurrent flow

Even number of tube passes

I t , - t l I T1-7-2

LMTDCrl, [ t 2 - t 1 1 a = -

where L M T D, , = Cocurrent flow L M T D

L M T D C n f = Uncorrected countercurrent flow L M T D

1 , t ,, T , T 2 , are defined in Paragraph T-4.42

t = T * L M T D ( F )

F = L M T D Correction Factor

The average tube fluid temperature may then be determined from the following equation:

where

T-4.46 OTHER CASES For cases involving nonlinear temperature-enthalpy profiles and/or pass geometries other than those given above, other methods must be used to establish mean metal temperatures. However, with the assumption of constant overall heat transfer rate, the following relationship always applies:

T - i = * L M T D ( F )

If one fluid average temperature can be established accurately, knowing the effective mean temperature difference allows the other to be determined.

-



T-4.5 SELECTION OF THE DESIGN CASE All foreseeable modes of operation should be considered when specifying the metal temperatures to be used for calculation of the equivalent differential expansion pressure. Consideration should be given to the following: (1) Normal operation, as specified by purchaser, under fouled conditions at the design flow rates

and terminal temperatures (2) Operation at less than the design fouling allowance (under such conditions, the purchaser

should supply details in regard to anticipated operating parameters) Other operating conditions to which the equipment may be subjected, as specified by the purchaser, may include, but are not necessarily limited to:

(1) Alternate flow rates and/or terminal temperatures as may be the case during start-up, shutdown, variable plant loads, etc.

(2) Flow of a process fluid or clean fluid through one side, but not the other The largest positive and negative values of equivalent differential expansion pressure generally correspond with the cases under which the largest positive and negative differential thermal growths occur; an exception being if varying values of material modulii of elasticity alter the comparison. The differential thermal growth between the shell and tubes is determined as follows:

AL = L, ( f f ,[ T , - 701 - ff T [ t M - 701)

where AL = Differential thermal growth between the shell and tubes, inches

L I =Tube length, face-to-face of tubesheets, inches

as =Coefficient of thermal expansion of the shetl, inches/inch/ F (see Table D-11)

Q, = Coefficient of thermal expansion of the tubes, inches/inch/ F (see Table D-11)

T-4.6 ADDITIONAL CONSIDERATIONS

T-4.61 SERIES ARRANGEMENTS Individual exchangers in series arrangements are generally subjected to different temperature conditions. Each individual exchanger should be evaluated separately. Alternately, all could be designed for the most severe conditions in the series.

T-4.62 OTHER MODES OF OPERATION If fixed tubesheet heat exchangers are to be operated under conditions differing from those for which the initial design was checked, it is the purchaser's responsibility to determine that such operation will not lead to a condition of overstress. This requires a full re-evaluation of required tubesheet thickness, shell and tube longitudinal stresses, tube-to-tubesheet joint loads, and flexible shell elements based on the new operating conditions.


THERMAL RELATIONS

FIGURE T-3.1

CHART FOR SOLVING LMTD FORMULA

SECTION 7

where GTTD = Greater Terminal Temperature Difference. LTTD = Lesser Terminal Temperature Difference.

Greater Terminal Temperature Difference NOTE-For points not included on this sheet multiply Greater Terminal Temperature Difference and Lesser Terminal Temperature Diffen

by any multiple of 10 and divide resulting value of curved lines by same multiple.


SECTION 7 THERMAL RE

FIGURE T-3.U

II

K


T

FIGURE T-3.2B

w 3 I- m

5 " 3

I



FIGURE T-3.2C

r

a

3 3 Ir,

z 0 l- 0 W

K 0 (3

0 I- = J

c

- a

W a 0 E t5g a

a. v) W vl v)

P d

W I v)

c3

a


S

FIGURE T-3.2D

W

3 m

a

SE 7

a

- 1


THERMAL R E ~ ~ ~ O ~ S

4 -

138

FIGURE T-3.2E

> c i

c

1 1

1

I! i;

$

q 0

= s o w


FIGURE T-3.2F

0 0 0 0 UO13WJ N01133U2403 O l W l : A

0

r 3

tn W tn tn a n m W

2 LL 0 K W rn E 3 Z Z W z W K 0 E U 0

ci

v) W v) tn 3 -I W I: tn co

##

K

H

0,


SECTION 7

140

THERMAL RELATIONS

FIGURE T-3.2G

51 0

0 0 ? 8

0 a 0

24013V4 NOLL33W03 cUIN1- 4

8 0

L 3 3 ;t

z 3

- L

.I.

L) 3 3= 5: 0 u P


THERMAL RELATIONS

FIGURE T-3.2H -

SECTION 7



FIGURE T-3.21

1 42 si :and

0

0 m m h Q O

_. d 0 0 0 0 .

ards Of The Tubular Exchanger Manufacturers

v) v) w z

w &

2 Lz w LL

t- 3 a

LL

Asso ciation

A t RELATIONS

FIGURE T-3.2J

v) W v) v)

0, W

a

m 2 L 0 K W m 5 3 z z W z v) v)

IL a

A W 2 vl

3 E3 n

5

LL

8 - >

v.4

11

a



FIGURE T-3.2K

U O l 3 V j NO11338803 O l W l = A



0 0 0 c 0

Standards Of The Tubular Exchanger Manufactur

v) v) w I w > c u W L L W

W & 3 t

& w h

t

-

a

5 n p.

v a

ers Associati on 145

0 a

;D a

L N01133S

THERMAL RELATIONS

FIGURE T-3.3A

U A / w c


THERMAL RE

FIGURE T-3.3B


THERMAL RELATIONS

FIGURE T-3.3C


SECTION 8 PHYSICAL PROPERTIES OF FLUIDS

(Note: This section is not metticated)

P-1 FLUID DENSITY

P-1 .I SPECIFIC GRAVITY OF LIQUID PETROLEUM FRACTIONS The specific gravities of liquid petroleum fractions and saturated light hydrocarbons are shown in Figure P-1 .l.

The general density nomograph Fig. P-1.2 permits the approximation of the density of organic liquids at temperatures between -1 50" F and + 500" F, if densities at two temperatures are known. Table P-1.2 lists the coordinates on the center grid for locating the reference points for 65 compounds. The reference point for a substance may be determined if the density is known for two different temperatures. The intersection point of the two straight lines joining the corresponding values of the known temperatures and densities is the desired reference point of the substance.

P-1.2 DENSITY OF ORGANIC LIQUIDS

P-1.3 COMPRESSIBILITY FACTORS FOR GASES AND VAPORS

The P - u - T relationships for gases and vapors may conveniently be expressed by the equation P u = Z R T , where Pis the absolute pressure, uis the specific volume, 7- is the absolute temperature, R is a constant which may be found by dividing the universal gas constant R by the molecular weight of the gas, and Z is the compressibility factor. Z has the value of unity for an ideal gas under all conditions and, therefore, is a measure of the extent of the deviation of a real gas or vapor from the ideal state. Figures P-l.3A, P-1.38, P-l.3C are generalized plots of compressibility factor as a function of reduced pressure, P 1 P cI and reduced temperature, ?- 1 T c. The dotted curves represent constant values of the pseudo-reduced volume u ' = u 1 ( R T / P ) where the subscript c refers to the critical value. These may be used to calculate pressure (or temperature) when the temperature (or pressure) and specific volume are known. If Pis expressed in pounds per square inch, vin cubic feet per pound, and T in degrees Rankine, the numerical value of R is 10.73. For critical property data, see Paragraph P-6.

P-2 SPECIFIC HEAT

P-2.1 LIQUID PETROLEUM FRACTIONS The specific heats of liquid petroleum fractions of various API gravities are shown as functions of temperature in Figure P-2.1. The specific heat versus temperature lines shown apply to virgin mid-continent stock and must be corrected for other stocks. An inset curve of this correction factor versus characterization factor is provided.

P-2.2 PETROLEUM VAPORS The specific heats of petroleum vapors of various characterization factors are shown as functions of temperature in Figure P-2.2.

The low pressure specific heats of a number of pure hydrocarbons are shown as functions of temperature in Figures P-2.3A, P-2.3B and P-2.3C.

The specific heats of miscellaneous liquids and gases at various temperatures may be read from the alignment charts, Figures P-2.4A and P-2.4B.

Specific heat data in Figures P-2.2, P-2.3A, P-2.3C and P-2.4B apply only at pressures low enough so that the specific heats are not significantly affected by pressure changes. At higher pressures, the specific heats may be substantially higher than the low pressure values. Figure P-2.5 is a generalized chart which may be used to calculate the approximate correction to the low pressure specific heat

P-2.3 PURE HYDROCARBON GASES

P-2.4 MISCELLANEOUS LlQUlDS AND GASES

P-2.5 GASES AND VAPORS AT ELEVATED PRESSURES


PHYSICAL PROPERTIES OF FLUIDS SECTION 8

for any gas at high pressure. The isothermal change in molal specific heat, A C = C - C *, is plotted against reduced pressure, P , with reduced temperature, T , as a parameter. Outside the range of the chart, the following empirical equations are accucate enough for most practical purposes. ForT,> 1 . 2 a n d A C , < 2 , A C , = 5 . 0 3 P r / T r , f o r T r < 1.2and A C < 2.5, A C , = 9 P / T 6 . For critical property data, see Paragraph P-6.1 and P-6.2.

P-3 HEAT CONTENT

Heat content of petroleum fractions, including the effect of pressure, are shown as functions of temperature and API gravity for various UOP K values in Figure P-3.1. The latent heats of vaporization of various liquids may be estimated by the use of Figure P-3.2. The recommended range of use is indicated for the compounds listed. See Table P-3.3 for heat capacity ratios for various gases.

P-4 THERMAL CONDUCTIVITY

P-4.1 CONVERSION OF UNITS Table P-4.1 gives factors for converting thermal conductivity values from one set of units to another.

P-4.2 HYDROCARBON LIQUIDS The thermal conductivities of liquid normal paraffinic hydrocarbons are shown in Figure P-4.2.

P-4.3 MISCELLANEOUS LIQUIDS AND GASES Tables P-4.3A and P-4.3B give tabulated values of thermal conductivrry for a number of liquids and gases at atmospheric pressure.

Thermal conductivity for gases at elevated pressure can be corrected by the use of Figure P-4.4A. Thermal conductivity for liquids at elevated.pressure can be corrected by the use of Figure P-4.4B. This chart is intended for use above 500 psia and when T T is less than 0.95.

P-4.4 GASES AND LIQUIDS AT ELEVATED PRESSURES

P-5 VlSCOSlTY

P-5.1 VISCOSITY CONVERSION A viscosity conversion plot, Figure P-5.1, provides a means of converting viscosity from Saybolt, Redwood or Engler time to kinematic viscosity in centistokes. The absolute viscosity in centipoises may be determined by multiplying the kinematic viscosity in centistokes by the specific gravity. Table P-5.1 gives factors for converting viscosity values to various systems of units.

The viscosities of petroleum oils having Watson and Nelson (UOP) characterization factors of 10.0, 11 .O, 11.8 and 12.5 are shown plotted against temperatures in Figures P-5.2A, P-5.2B, P-5.2C and

P-5.2 PETROLEUM OILS

P-5.2D.

P-5.3 LIQUID PETROLEUM FRACTIONS Figures P-5.3A and P-5.3B give viscosity data for a number of typical petroleum fractions plotted as straight lines on ASTM viscosity charts. These charts are so constructed that for any given petroleum oil the viscosity-temperature points lie on a straight line. They are, therefore, a convenient means for determining the viscosity of a petroleum oil at any temperature, provided viscosities at two temperatures are known. Streams of similar API gravity may have widely different viscosities; therefore, values of viscosity shown here should be considered as typical only.

P-5.4 MISCELLANEOUS LIQUIDS AND GASES The viscosities of certain liquids are shown as functions of temperature in Figure P-5.4A. The viscosities of certain gases and vapors at one atmosphere pressure are given by Figure P-5.4B.



P-5.5 EFFECT OF PRESSURE ON GAS VISCOSITY Figure P-5.5 is a generalized chart which may be used to estimate the viscosities of gases and vapors at elevated pressure if the critical temperature and pressure and the viscosity at low pressure are known. The viscosity ratio, p / p n l m , is plotted against reduced pressure, P , with reduced temperature, T , as a parameter, where, patmand p are respectively the viscosities at atmospheric pressure and at pressure P. For critical property data, see Paragraph P-6.

P-6 CRITICAL PROPERTIES

P-6.1 PURE SUBSTANCES Table P-6.1 gives values of the molecular weights, critical temperatures, and critical pressures for a variety of pure compounds. For the calculation of compressibility factor, it is recommended that the critical pressures and temperatures of hydrogen, helium, and neon be increased by 118 psi and 14.4" R respectively.

P-6.2 GAS AND VAPOR MIXTURES Figures P-1.3, P-2.5, and P-5.5 may be used to estimate the properties of gas mixtures as well as pure substances if pseudo-critical properties are used in place of the critical values. The pseudo-critical temperature and pressure are defined as follows: T T c i -+ Y P p . c , = Y , P c* -+ Y

I c , = Y T c2 + . . . . # . . . . + YnTcn P c2 + . . . . . .. * . + YnPcn

where Y , Y 2 , etc. are the mole fractions of the individual components and T ci , T c 2 , etc., and P c i , P c 2 , etc. are their critical temperatures and pressures.

P-7 PROPERTIES OF GAS AND VAPOR MIXTURES To estimate properties of a gas or vapor mixture for which the individual component fractions and properties are known, the following formulas may be used:

P-7.1 SPECIFIC HEAT C p m l x = x , c p ] + x2cp2+ ..t......*l.. + X N C p ,

P-7.3 VlSCOSlTY

where, for component "N 'I:

x, =

M , =

C p N = K , =

CLN =

Y N =

Weight Fraction Mole Fraction Molecular Weight Specific Heat Thermal Conductivity Viscosity


PHYSICAL PROPERTIES OF FLUIDS SECTION 8

P-8 SELECTED REFERENCES (1) Reid, R. C. and Sherwood, T. K., "Properties of Gases and Liquids", 2nd Ed., McGraw-Hill Book

(2) Comings, E. W., "High Pressure Technology", McGraw-Hill Book Company, Inc., New York, 1956. (3) Hougen, 0. A,, Watson, K. M., Ragatz, R. A., "Chemical Process Principles", Part 1, 2nd Ed., John

(4) Tsederberg, N. V., 'Thermal Conductivities of Gases and Liquids", The M.I.T. Press, Massachusetts

(5) Yaws, C. L., "Physical Properties, Chemical Engineering", McGraw-Hill Book Company, Inc., New York,

Company, Inc., New York, 1966.

Wiley & Sons, Inc., New York, 1956.

Institute of Technology, Cambridge, Massachusetts, 1965.

1977. (6) Gallant, R. W., "Physical Properties of Hydrocarbons", Vol. 1 & 2, Gulf Publishing Co., Houston, Texas,

1968.



FIGURE P-1.1

i n W W a 6 W 0

I &

0

tb 0 W

c - Ic W a. x w c

- a


PHYSICAL PROPERTIES OF FLUIDS

D

6.5

5.5

5.0

0.5 4.0

Compound Acetic Acid Acetone Acetonitrile Acetylene Ammonia lsoarnyl alcohol Ammine Benzene n-Butyric acid Isobutane lsobutyric acid Carbon dioxide Chlorobenzene Cyclohexane n-Decane n-Dedecane Diethylamine n.Elconane Ethane Ethanethiol Ethyl acetate ' Ethyl alcohol

FIGURE P-1.2

GENERAL DENSITY NOMOGRAPH

01 U

M K

If! 250 .- Y

5

8 200

Y) lv

M E

SECTION 8

T

TABLE P-1.2 -100 -150 X AND Y VALUES FOR DENSITY NOMOGRAPH

X Y 40.6 93.5 26.1 47.8 21.8 44.9 20.8 10.1 22.4 24.6 20.5 52.0 33.5 92.5 32.7 63.0 31.3 78.7 13.7 16.5 31.5 75.9 78.6 45.4 41.7 105.0 19.6 44.0 16.0 38.2 14.3 41.4 17.8 33.5 14.8 47.5 10.8 4.4 32.0 55.5 35.0 95.0 24.2 48.6

Compound Ethyl chloride Ethylene Ethyl ether Ethyl formate Ethyl propionate Ethyl propyl ether Ethyl auindo Fluorobenzene n-Heptadecane nMeptane n-Hexadecane n.Hexane Methanethiol Methyl acetate Methyl alcohol Methyl n-butyrate Methyl isobutyrate Methyl chloride Methyl ether Methyl ethyl ether Methyl formate Methyl propionate

X Y 42.7 62.4 17.0 3.5 22.6 35.8 37.6 68.4 32.1 63.9 20.0 37.0 25.7 55.3 41.9 87.6 15.6 45.7 12.6 29.8 15.8 45.0 13.5 27.0 37.3 59.5 40.1 70.3 25.8 49.1 31.5 65.5 33.0 64.1 52.3 62.9 27.2 30.1 25.0 34.4 46.4 74.6 36.5 68.3

Compound Methyl sulfide n.Nonane n.Octadecane n-Octane n.Pentadecane n.Pentane n.Nonadecane I so pen ta ne Phenol Phosphine Propane Propionic acid Piperidene Propionitrile Propyl acetate Propyl alcohol Propyl formate n-Tetradecane n-Tridecane Triethylamine n-Undecane

Ref: Othmer, Josefowitz & Schmutzlcr, Ind. Engr. Chem. Vol. 40.5,883-5


?! a e n

c

P)

E, c

X Y 31.9 57.4 16.2 36.5 16.2 46.5 12.7 32.5 15.8 44.2 12.6 22.6 14.9 47.0 13.5 22.5 36.7 103.8 28.0 22.1 14.2 12.2 35.0 83.5 27.5 60.0 20.1 44.6 33.0 65.5 23.8 50.8 33.8 66.7 15.8 43.3 15.3 42.4 17.9 37.0 14.4 39.2 __

155

SECTION 8 PHYSIC

FIGURE P-1.3A

156

s 0

a 0

m 0

$=z ‘uo13Vd AllllalSS3tldW03 ~



FIGURE P-l.3B

n 6

i 6


SECTiON 8

rz'

W- K

7 W a n n

n a

W 0 3 W

157

158

FIGURE P-l.3C


PROPERTIES OF

FIGURE P-2.1

SE

0 1w 200 300 400 500 600 7w 800 900 1wo 1100 1200

TEMPERATURE - DEGREES F.


SECTION 8

0.90

0.85

0.80

0.75

0.70

0.65 I; W W 11:

0.60

X ui a \ 3 I- 0.55 m I-

I 3

0.50 0 k

n 2 m

0.43

0.40

0.35

0.30

0.25

0.20

160


FIGURE P-2.2

SPECIFIC HEATS OF PETROLEUM FRACTIONS

I

LINES OF CONSTANT WATSON REFERENCE

CHARACTERIZATION FACTOR = FALlON 6 WATSON, NATIONAL PETROLEUM NEWS sp. GR @ 60"

Trr = MEAN BOILING POINT, DEG. RANKINE JUNE 7, 1944 PGS R372, R375 ,__

/I I I I l l I I I I I I I I I ( D E G . R = D E G . F + ~ M ) ) 1 ; 1 1 1 1 i 1 1 1 i 1 i i i i 1 i i i 1 1

111 1 1 1 1 1 1 1 I I I I 1 I I I I I I I I I I 1 I l l l i l 1 1 L - 0 100 2W 300 400 Ma 400 700 800 900 loo0 1100

TEMPERATURE - DEGREES F.



FIGURE P-2.3A

SPECIFIC HEATS

N-PARAFFINIC GASES

A P I PROJECT 44 NATIONAL BUREAU OF STANDARDS

0 100 200 300 400 500 600 700 800 900 loo0 I 1 0 0 1200 TEMPERATURE DEGREES F.



FIGURE P-2.3B

SPECIFIC HEATS

N-MONO-OLEFINIC GASES

A P I PROJECT 44 N A T I O N A L BUREAU OF STANDARDS

0 100 200 300 4fm 500 600 7M) a00 900 lo00 1100 1200 TEMPERATURE DEGREES F.


P HY S I CAI,

FIGURE P-2.3C

0 850

0 800

0 750

0 700

0 650

LL

W 0600 W a:

0 s

SPECIFIC HEAT

AROMATIC AND CYCLO-PARAFFINIC

0 2 0 0 , - . . . . . . - . . I . . - . 0 1w 200 300 400 5 0 0 6 0 0 700 8W m looa 1100 1200

TEMPERATURE DEGREES F.


SECTION 8

DEG F

164

4 0 0

200

100


FIGURE P-2.4A

S P E C I F I C H E A T S OF LIQUIDS 40 LlQUiD 29 ACETICACID 100% 32 ACETONE

p 6 %?E:ACOHOL AMYL ACETATE 30 ANILINE 23 BENZENE 27 BENZYL ALCOHOL 10 BEN YLCHLORIDE

49 BRlrIfE ,2590 Co C12 51 BRINE,25% Na c\ 44 BUTYL ALCOHOL

2 CARBON DlSULPHlDE 3 CARBON TETRACHLORIDE 8 CHLOROBENZENE 4 CHLOROFORM

21 DECANE 6A DICHLOROETHANE 5 DICHLOROMETHANE 15 DIPHENYL 22 DIPHENYLMETHANE 16 DIPHENYL OXIDE 16 DOWTHERMA 4 ETHYL ACETATE

12 ETHYL ALCOHOL 100% 46 ETHYLALCOHOL 95% 50 ETHYLALCOHOL 50% 25 ETHYL BENZENE

1 ETHYL BROMIDE 13 ETHYL CHLORIDE 36 ETHYLETHER 7 ETHYL IODIDE

39 ETHYLENE GLYCOL

4NGE LEG

20- 50 - 70- 50

0- 130' 10- 00 - 20- 30

-30- 30 -40 - 20 -40- 20

0- 100 -100- 25

10- 60 0- I00 0- 50

-80- 25 -30- 60 -40- 50

80- 120 30- 100 0-200 a- 200

-50- 25 30- 80 20- 80 20- 80 0- I00 5- 25

-100 2 0- 100 - 40- 200

-30: 4g

-

SPECIFIC HEAT

4O 04A a3

5 0

a4

u: a5 UJ

UJ pc

Q X

m

U-

By permission from Heat Transmission, by W. H. McAdams.

0 49

0 50

52 0

Copyrighted

a7

53 0

1954. McGraw-Hill Book Company,


Inc.


7 0

8 0

I4 BU

0 I6

Deg F

- - - r 2.0 - - - - - - - - - 1.0 - 0.9 - Q8 - Q7

- 0.6

- - -

FIGURE P-2.4B

30

32 31 0

33 0-

3 4 0 -

35 0

36 0

S P E C I F I C H E A T S - G A S E S 1 A T M .

- .-

$0.2 - - - -

- - - 0.1

0.09

- 0.07

- Q06 - QOS

= a08

- -

C = Specific heof= Btu/(Lb)(Deg F ) = P c u / ( Lb)(DeqC)

I

4 ETHYLENE I 1 81 :: 13

I7 B 17C 17A I7 D

I 2

35 30 20 36 19

FRE~N-II (CCI FI FREON-21 KH?I,F) FREON22 (CHCI F ) FREON-I13(CCI,F ~ C 2 I F2) HYDROGEN

HYDRCGEN BROMIDE HYDROGEN CHLORIDE HYDROGEN FLUORIDE HYDROGEN IODIDE HYDROGEN SULPHIDF

21 5 METHANE 6 1

25 NITRIC OXIDE 28 1,

26 NITROGFN 23 OXYGEN

3 5 6 48 0 9 0

32 - 390 390- 7 5 0 7% - 1 5 5 0 32 -2550 32 - 1110

I I10 - 2 5 5 0

32 - 2 5 5 0 32 - 390

3 9 0 - 1 1 1 0 i l l0 - 2 5 5 0

32 - 390 390 - Ill0

I I I0 - 2550 32 - 300

O I I 100 0

17C 780° 0

17 D

32 - 300 32 - 3'30 32 - 3 0 0 52 - 1110

itlo - 2 5 5 0 32 - 2 5 5 0 32 - 2 5 5 0 $2 - 2 5 5 0 32 - 2 5 5 0 32 - 1290

1'290- 2 5 5 0 32 - 5 7 0

570 - 1290 1290 - 2 5 0 0 32 - I290

1290- 2 5 5 0 32 - 2 5 5 0 32 - 930 930 - 2550 510 - 2550

32 - 7 5 0 750 - 2550

32 - 2550

SECTION 8

12 0 0 15

18 0

?2 0

BY permission from Heat Transmission, by W. H. McAdams. Copyrighied 1954. McGraw-Hill Book Company. Inc.


8 s

FIGURE P-2.5

I I ] Cp’ Molol Heat Copocity at low Pressure I

0.02

I Pr Reduced Pressure pc

0.0 1 0.1 0.2 0.4 G.6 0.8 1.0 2 4

___

Reprmled by permission from Industrial and Enqlneerlnq Chemistry. vof 49. p 121. 1957 A H W e t s a n d bffe


s

FIGURE P-3.1

HEAT CONTENT OF PETROLEUM FRACTIONS INCLUDING THE EFFECT O F PRESSURE

U c 4, r

TEMPERATURE, "F

Reprinted by permission of Shell Development Compony. Copyright 1945

Standards Of The Tubular Exchanger Manufacturers Association 1 67

SECTION 8

._

X

5.6 4.0 3.2 6 .O 3.6 2.6 3.6 3.4 2.0 1.7 6.9 5.6 3.9 3.3 3.5 3.6 1.5 3.7 9.4 4.8 2.2 3.8 0.8 3.1 6.2 4.0 3.1 4.7 3.9 4.1 3.0 4.0 3.1 1.8 3.6 3.9 3.3 4.0 3.5 3.5 3.4 3.4 5.2 3.3 3.6 4.1 2.6 5.2 1.9 1 .o 1.2 5.6 3.6 3.3 3.2 4.3 2.1 3.5 2.3 2.0 1.5 6.0 3.0

-

-


Range tc-toF

212-392 284-464 176-392 392-572 50-572

104-158

167-345 337-572 302-392 392.517 337-517 302-392

284-527

212-392 345408 392-572

158.392

50-2 12

50-572

256.392 50- 90 90-302

302-752 176-643 643-932

50-266 50-284

285-482

302446 50-122

59-266 266-464 158482 140-302 176-427 122-320 194482 113-392 50.517

131464 50-194 68-285

283-464 212-392

61-230 230-247 302-482 302-482 43- 77 77-256 61-572 59-482 50-392

77-517

446-661 2 12-392 212-572 355-582

50-675

266-446

122-256

59-482

302-482

168

- Y

11.9 10.3 3.8 9.4

12.5 11.6 11.7 12.1 9.8 9.7 7.7 8.8 9.5

11.1 13.7 17.3 14.5 15.7 13.3 8.8

15.2 15.2 12.8 15.5 14.5 9.8 7.0 6.3 9.0

12.2 9.3 0.6

12.7 12.7 17.2 17.2 15.4 15.1 18.7 18.7 13.5 13.2 8.3 5.3 4.7 6.5

11.1 11.2 11.3 13.7 9.2

12.3 13.8 12.7 12.7 11.c

8.E 8.3

12.5 12.3 13.7 15.9

1.C

-

-

FIGURE P-3.2

LATENT HEATS OF VAPORIZATION OF VARIOUS LIQUIDS - t,. “F 509 155 !72 585 552 307

273 548 508

508 455 91

522 542 291 506 468 329 982

-

952

895 470

362 369

5c

382

382 232. 325 205 417 293 512 456 116 464

315 289

417 421

97

565 386 37c 205 507 4 5f 652 314 611 52C 707 -

LIQUID

Acetic Acid Acetone 4mmonia Amy1 alcohol (-is01 Benzene Butane (-n) Butane Butane (-is01 Eutyl alcohol (-n) Butyl alcohol (-1s0) Eutyl alcohol Butyl alcohol (-set) Butyl alcohol (-tert) Carbon dioxide Carbon disulfide Carbon tetrachloride Chforrne Chloroform Dichloroethylene ( cie) Dimethyl amine Diphenyl Diphenyl Diphenyl Diphenyl oxide Diphenyl oxide Ethane Ethyf alcohof Ethyl alcohol Ethyl amine Ethyl chloride Ethylene Ethylene Ethyl ether Ethyl ether Freon-11 (CCIJF) Freon.12 (CCkFd Freon-21 1CHCI:F)

1800 1700 3 1600 - 1500 - 1300 - - 1 1 0 0 - 1000 - 900 - 800 - 700 - m--

- - - - - -

500 - - 400

Freon-22 (CHCIFd Freon-1 13 (CCkFCCIFa) Freon-114 (CCIFKXIFi

50

L - 60 - 70 - 80 - 90

- 100 -110

- - - - - - - 130 - - -160

- 180 - 200 - - - - - -

Heptane (-n) Hexane (-nf Methane Methyl alcohol Methyl alcohol Methyl amine Methyl chloride Methyl chloride Methyl formate Methylene chloride Nitrous oxide Nitrous oxide Octane (.n) Pentane 1-n) Pentane (-iso) Propane Pmpyl alcohol (-n) Propyl alcohol (-is01 Pyridine Sulfur dioxide Toluene Trichloroeth ylene Water

4.4 - L - * - - -

200 - 180 - 160 - m

- - 130 - - - 100 - - 90 - - 80 - 70 - M I -

50-

- - m

40

400 - -500 - -400

- 700

- 800 -900

- lo00 -1100

- 1300 -1500

- - - -

- - - - - 1800

- - - - 20 - -

Y

0 1 2 3 4 5 6 7 8 9 1 0

X

Example:-For water at 212’F, t,-t = 707-212 = 495 and the latent’heat per Ib is 970 Btu

(Latent heat accurate within t. 10 per cent)

From ”Process Heat Transfer.” 1st Ed., Donald Q. Kern; McGraw-Hill Book Company, reprinted by permission


TABLE P-3.3 HEAT CAPACITY RATIOS (C / C

Btu Btu cal kg-cal watts

hr-sq fi-deg F per in. hr-sq Il-deg F per ft sec-sq cm-deg C per cm hr-sq m 4 e g C per m sq cm-deg C per cm

1 0.08333 3.445 x lo-' 0.1240 1.422 X lo-' Btu h r - s q ft-deg F per in.

r

Acetylene Air Ammonia Argon Benzene Carbon Dioxide Chlorine Dichlorodiflouromethane Ethane Ethyl Alcohol

Ethyl Ether Ethylene Helium

Hexane (n-) Hydrogen Methane Methyl Alcohol Nitrogen

Oxygen Pentane (n-) Sulfur Dioxide

12.00 Btu hi-sq ft-deg F per f t

cal sec-sq cm-deg C per cm 2,903

1.26 1.403

1.310 1.688

1.10 (200 O F)

1.304 1.355

1.139 (77 OF)

1.22

1.13 (200°F)

1.08 (95 O F) 1.255

1.660 (-292 O F) 1.08 (176 F)

1.410 1.31

1.203 (171 O F) 1.404 1.401

1.086 (189 O F) 1.29

1 4.134 X lo-' 1.488 0.0 173 1

24 1.9 1 360 4.187

(All values at 60 O F and one atmosphere unless otherwise noted)

8.064 kg-cal hr-si m-deg C per m

TABLE P-4.1

0.6720 2.778 x 10-3 1 0.01 163

THERMAL CONDUCTIVITY CONVERSION FACTORS TO convert the numerical value of a property expressed in one of the units in the left-hand column of the table to the

numerical va lue expressed in one of the units in the top row of the table, multiply the former value by the factor in the block comnion to both units.

693.4 watts sq c m - d e g C per cm 57 78 0.2388 85.99 1


FIGURE P-4.2

.13 THERMAL CONDUCTIVITY OF NORMAL PARAFFINIC HYDROCARBON LIQUIDS

12

11

10

09

08

.07 _I . . . . # _ . . I

....,

. .

... : /

: : . : I

..::

. . . . ,

. . . )

. . .

. . . )

. . . . .. . ....

. . . .... . . . . .... . _ i . . . . / _ . . . . .

. . . .05

.04 -300 -200 -100 0 100 200 300 400


FIGURE P-4.3A

T, "F k Liquid T, "F Liquid

-110 68 092 Formaldehyde Acetic Acid 0 300 078 0 093 68 Acetone 68

170 076 Glycerine -220 137 390

50 Acetylene -110 089 Heptane (N)

300

k

185 132 116 161 181 074 050

1 1;; I Acrylic Acid

095 092 ,089 085 133 089 085 059 065 059 082 056 100 087 077 075 104 064 084 072 07 1 052 075 068 083 056 075 050 089 08 1 060 ,066 063 058 088 065 110 080 080 045

Ally2 Alcohol

Amy1 Alcohol

Aniline

Benzene

Bromobenzene

Butyl Acetate (N)

Butyl Alcohol (?SO)

Hexyl Alcohol

Methylethyl-Ketone (MEK)

Methyl Alcohol (Methanol)

Nonane (N)

O d a n e

Para Xylene

Pentane

Propyl Alcohol (N)

Propyl Alcohol (ISO)

Toluene

Trichloroethylene

Vinyl Acetate

Water

Xylene (Ortho)

Xylene (Meta)

Butyl Alcohol (N)

Carbon Disulhde

Carbon Tetrachloride

Chlorobenzene

Chloroform

Cumene

Cyclohexane

68 250

0 250

-22 300 50

300 50

300 68

176 390 50

250 -40 300

-40 140 300 32

390 -40

86 300 32

230 32

100 200 300 420 620 32

176 390 32

176 390

Dichlorodifluoromethane

077 074 089 067 132 096 077 056 076 054 076 065 047 069 048 106 072 092 075 072 083 050 084 065 046 088 065 343 363 383 395 376 275 087 068 048 080 062 044

Ethyl Acetate

Ethyl Alcohol

Ethyl Benzene

I JLU I . U O U l l l i

Extracted from "Physical Properties of Hydrocarbons" By R. W. Gallant, Copyright 1968, Gulf Publishing Co.

68 212 68

212 68

300 68

320 32

390 32

320 -40

50 160 300 -40 300

-1 12 68

-1 12 212

32 390

-100 212

32 390 40

100 250 -80

50 140 32

230 -40 300 32

390 -


SECTION 8

-32e


-148

FIGURE P-4.3B

THERMAL CONDUCTIVITIES OF GASES AND VAPORS [k = BTU:(hr)(sq ftHdeg. F per ft)]

.0057

.0108

.O 140

.0126

.0095 ,0052 .0078

Substance

.0076 .0099 .O 157

.0140 .0172 .0184 .0224 .0192 .0280 .0123 .0148

,0075 .0103 .O 166 .O 135

TEMPERATURE ' F. 32 I 122 I 2 12 I 392

.0037

572 I 752

.0064'

.0088

.0139

.0128

Acetone Acetylene Air Ammonia Arson

.0177

.0042

.0047

.0064

.0074

.0101

.0131

.0056

.0091

.Oil97 *

.0063

.0176

.0052 .0068

.0058 .008 1

.0094 .0080 .0115 .0175 .0096 .O 150 .O 124 .0095 .0145 ,0131 .0200 .0161

.0040

.0080i

.0068i

.0074

.0050

.0161

.0260

-0988 .0103 .0112

.0109

.I240 .1484

.0197 -0255 .0358

-0128 .0094 .O 140 .0063 .0091

.0181 .0220

.0138 .0040

.0089

.009 1 -0047

Benzene Butane (n-1 Butane (is04 Carbon dioxide Carbon disulfide Carbon monoxide Carbon tetrachloride Chlorine Chloroform Cy clohexane Dichlorodifluoromethane Ethane Ethyl acetate Ethyl alcohol Ethyl chloride Ethyl ether Ethvlene

.0080

.0084 ,0040 .0134

.0043

.0038

.0048

.0106

.008 1

.0055

.0077

.0101 .0338 .06 12 Helium

Heptane (n-) Hexane (n-) Hexene Hydrogen Hydrogen sulfide Mercury Methane Methyl acefafe Methyl alcohol Methyl chloride Meihvlene chloride

.0818

.0072

.006 1

.0966

.0076

.0176

.0059

.0083

.0053

.0039

.0026

.O 138

.O 139

.0088

.0652

.0109 .0490 1 .0255 .0287 J Neon

Nitric oxide Nitrogen Nitrous oxide Oxygen Pentane (n-) Pentane (iso-) Propane Sulfur dioxide Water vapor,

* Value a! - S8* F. t Value a! 68" F.

zero pressure

.0038 I .0091 .0142 I .0166 I .0188 I

I .0136 I .0182

Adapted from Heaf Transmission, by W. H. McAdams. Copyrighted 1954. McGraw-Hill Book Company, Incorporated.



FIGURE P-4.4A

Standards Of The Tubular Exchanger Manufacturers A s s ~ ~ ~ ~ t ~ ~ ~ 173

8

16

15

14

13

12

11

10

9

8

7

6

174

HYSiCAL PRO

FIGURE P-4.4B

THERMAL CONDUCTIVITY-LIQUIDS PRESSURE CORRECTION-GENERALIZED CORRElATlON

REF.: LENOIR, J. M., PET. REF. 36, 162-164 (1957)

Note: To find thermal conducticity kz at pressure P? and temperafure T, multiply known value kl by ratio

Where: k, k. ex e..

PI and P: P, = Critical Pressure, PSlA

= Known thermal conductivity a t ony pressure PI and temperature T = Desired thermal conductivity at P2 and T = Thermol conductivity foctor at (Pr)l and T, = Thermal conductivity factor at (Pr)2 and T, = Pressures, PSlA

(P,)] =: PI/P,, Dimensionless (Pr)D = PdP,, Dimensionless T To I= Critical temperoture, R T, = T/Tc, dimensionless

= Temperature, "R ( = 4050 4- OF)

0 1 2 3 4 5 6 7 8 9 10 11 12



Ib - Ib-sec - Ib - gm poises = -

cm-sec ft-sec ft* ft-hr

01 000672 0000209 2 42

1 0672 00209 242

14 88 1 031 1 3600

479 32 2 1 116000

00413 000278 00000864 1

98 1 6 59 2048 23730

SECTION 8

kg-sec

m2 I_

000 102

0102

1517

4 88

000042 1

1

TABLE P-5.1

centipoises

gm poises = -

cm-sec

lb

ft-sec

Ib-sec

-

ft'

ib

ft-hr

kg-sec

m2

___

-

centiporses

1

100

1488

47900

413

9810

To convert the numerical value of a property expressed in one of the unlts in the left-hand column of the t ab le to the numerical value expressed in one oi the units in the top row of the table. multiply the former value b y the factor in the block common to both units

FIGURE P-5.1

V I S C O S I T Y C O N V E R S I O N P L O T ENGLER DEGREES

ESE CURVES ARE DRAWN TO FIT THE FOLLOWtN' UATIONS WHICH MAY BE USED FOR EXTRAPOUT01 YOND THE RANGES PLOTTED.

(I) SAYBOLT UNIVERSAL FROM EXPERIMENTAL DATA SAYBOLT UNIVERSAL K X A - I

WHEN K ~ 7 0 THEN THEN A-4.620@lm*F A-4.629@lJO:F THEN A-4.652@210 F

(2) SAYBOLT FUROL

(3) REDWOOD NO. 1 K-0.2641- WHEN t-40 TO 85 SEC.

(3) REDWOOD NO. 1

(4) REDWOOD NO. 2

(5) ENQLER TIME

(6) ENCLER DEGREES K-EX7.6('-&)

FROM EXPERIMENTAL DATA 190

K-0.2471- f WHEN 1-85 TO 2ooo SEC. I-l/tOXREDWOOD NO. 1 TIME

K - l m ( .001471-7) . . OR t - S E 3.74

K - KINEMATIC VISCOSITY-CENTISTOKE. t -TIME OF EFFLUX-SECONDS E - ENGLER DEGREES

REFERENCES- S A Y M L T UNIVERSAL-A.S.T.M. P W C E E D I N W 37-1411

SAYBOLT FUUOL-KANSAS CITY TESTINO LAB. BULL '25 p u I R E W O D NO. 1-INST. OF PET. TECH. S T A N D A R D METHOD8

REOWOOD NO. ?--D1110. p IH

O L N E R A L 4 A R N E R 4 K E L L Y J . APF'.PMYS~CS.~.Y~~~Y~!~

C3.T.M. TENTATIVE S T A N D A R D -1

3RU. OD. 1s35 P 170.

:%g: &%E$R"%&%%?E!'? % k W 1 $ N O , €0. 1-

I0 I00 500 1000 so00 I O * . ~

TIME IN SECONDS-SAYBOLT (UNIVERSAL 6 FUROL), REDWOOD Nos. 1 (L P, ENGLER TIME


PHYSfCAL P

FIGURE P-5.M

V I S C O S I T Y - T E M P E R A T U R E R E L A T I O N S H I P F O R P E T R O L E U M O I L S LINES OF CONSTANT DEGREES A.P.I. CHARACTERIZATION FACTOR, K = 10.0

Ref: Watson. Wien 6 Murphy, Industrial 6 Engineering Chemistry 28,605-9 (1936)

U 0

w U 3 t- 4 U w Q

t- 3

FIGURE P-5.2B

V I S C O S I T Y - T E M P E R A T U R E R E L A T I O N S H I P F O R P E T R O L E U M OILS LINES OF CONSTANT DEGREES A.P.I. CHARACTERIZATION FACTOR. K = 11 .O

Ref: Watson, Wien 6 Murphy, Industrial 6 Engineering Chemistry 28,605-9 (1936)

U

w U 3 12

5 a w 0

t


PHYSICAL PR S

FIGURE P-5.2C

V I S C O S I T Y - T E M P E R A T U R E R E L A T I O N S H I P F O R P E T R O L E U M O I L S LINES OF CONSTANT DEGREES A.P.I. CHARACTERIZATION FACTOR, K = 11.8

R e f . Watson, Wien 6 Murphy, Industrial 6 Engineering Chemistry 28,605-9 (1936)

FIGURE P-5.m V I S C O S I T Y - T E M P E R A T U R E R E L A T I O N S H I P F O R P E T R O L E U M O I L S LINES OF CONSTANT DEGREES A.P.I. CHARACTERIZATION FACTOR, K = 12.5

Ref: Watson. Wien 6 Murphy, Industrial 6 Engineering Chemistry 28.605-9 (1936)


I

INS

I O w w 50,000 20,000 I0,OOO

v)

5 75 2

tv ., - Reprinted by permission of the copyri ht owner, &so Research and Engineering Co., Linden, N. I. , from ”Data Book on Hydrocarbons,” by I. B. Maxwell. D. Van Nostrand Company, s e w York. 1950.


FIGURE P-5.3B


- NO. I 2 3 4 5 6 7 8 9 10 I1 12 13 I4 IS 16 I7 18 19 20 21 22 23 24 25 20 27 28 20 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 f( 5s

-

-

100 -- 901- 60-1

70 - - 60

50

40

3 0 _ -

20- -

10 - - * - -

Liquid AwWdebydr

210 -- 200 190

' 6 0 .- 150 - - 140 * - 130 -- 120 - - 110 -- 100

- 90 80 7o

.- 60 50

.- 4 0 30

Awtic acid. 100% Amtic acid. 70 % Awtic anhydride Aatone, 100% Acetone. 35 % huyl alcohol Ammonia. 100% Ammonia. 26% Amy1 acet.ta Amy1 alcohol Aniline Anisole Anenic trichloride Bensene Brine, CaCIi, 25 % Brine, NaCI, 25% Bromine Bromotoluene Butyl acetate Butyl alcohol Butyric acid Carbon dioxide Carbon disulphide Carbon tetrachloride Obiorobenxene Chloroform Zhlorosultonic acid Zhlorotoluene, ortho Chlorotolucne. met. >hlorotoluene para Crasol, mela Cyclohexanol Dibromoethane Dichloroethane Dichloromethane Diethyl oxalate Dimethyl oxalate Diphenyl Dipropyl oxalate Ethyl acetate Ethyl alcohol. 1Ooc; Ethyl alcohol. 95 % Ethyl alcohol. 40% Ethyl benzene Ethyl bromide Ethyl chloride Ethyl ether Ethyl formate Ethyl iodide Ethylene 6lYCOl Formic acid Freon-1 1 Freon-12 Freon-21

_c

X 15.2 12.1 9 .1 12.7 14.5 7.9 10.2 12.6 LO. 1 11.8 7.5 8.1 12.3 13.9 12.5 6.0 10.2 14.2 M . 0 12.3 8.6 12. I 11.0 10. I 12.7 12.3 14.4 11.2 13.0 13.3 13.3 2.5 2.9 12.7 13.2 14.6 11.0 12.3 12.0 10.3 13.7 10.5 9.8 6.5 13.2 14.5 14.8 14.5 14.2 14.7 6.0 10.7 14.4 16.8 15.7

-

-

- Y

14.2 17.0 12.8 7.2 15.0 14.3 2.0 13.9 12.5 18.4 18.7 13.5 14.5 10.9 15.9 16.0 13.2 15.9 11.0 17.2 15.3 0.3 7.5 13.1 12.4 10.2 18. I 13.3 12.5 12.5 20.8 14.3 15.8 12.2 8.9 10.4 15.8 18.3 17.7 9.1 13.8 14.3 16.6 11.5 8.1

5.3 8.4 10.3

15.E 9.C 5.e 7.:

- 4.a

6 . 0

23.8

-

No. I_

50 57 58 59 80 01 62 63 64 65 66 07 08 09 70 71 72 73 74 75 70 77 78 79 80 81 82 83 84 85 86 87 88 89 90 91 92 93 94 95 88 97 98 99 100 101 I02 103 104 105 1W 107 108 108 110 -

Liquid Freon-22 Freon-I13 Glycerol, 100% Glycerol. 50 % Hcptene Hcxane Hydrochloric acid, 31.54 Isohutyl alcohol Isobutyric acid Isopropyl alcohol Kermne Linsccd oil, raw Mercury Methanol, 100% Methanol. 90% Methanol. 40 X Methyl acetate Methyl chloride Methyl ethyl ketone Naphthalrne Nitric acid, 95 5 Nitric acid. 80 5 Nitrobmrcne Nitrotoluene Octane Dctyl alcohol Pentachloratham Pcntanc Phenol Phosphorus tribromide Phosphorus trichloride Propionic acid Ptopyl alcohol Propyl bromide Propyl chloride Propyl iodide Sodium Sodium hydroxide, 50 75 Stannic chloride Sulphur dioxide Sulphuric acid, 110% Sulphuric acid, 98% Sulphuric acid, 1305 Sulpburyl chloride Tetrachlorocthme Tetrachlorathylene Ti-nium tctrachloridt Toluene Trichloroethylene Turpentine Vinyl acetate Weter Xylenc. ortho Xylene. metn Xylene. para

By permission from CHEMICAL ENGINEERS' HANDBOOK. by I . H. Perry. Copyrighted 1950. McGraw-Hill Book Company, Inc.

- X I7 2 12.5 2.0 6.9 14.1 14.7 13.0 7.1 12.2 8.2 10.2 7.5 18.4 12.4 12.3 7.8 14.2 15.0 13.9 7.9 12.8 10.8 10.8 11.0 13.7 6.6 10.9 14.9 0.9 13.8 16.2 12.8 9.1 14.5 14.4 14.1 16.4 3.2 13.5 15.2 7.2 7.0 10.2 15.2 11.9 14.2 14.4 13.7 14.8 11.5 14.0 10.2 13.5 13.9 13.9

-

-

- Y 4.7 11.4 30.0 19.6 8.4 7.0 10.6 18.0 14.4 16.0 16.9 27.2 16.4 10.5 11.8 15.5 8.2 3.8 8.8 18. I 13.8 17.0 10.2 17.0 10.0 21.1 17.3 5.2 20.8 10.7 10.9 13.8 16.5 9.8 7.3 11.6 13.9 25.8 12.8 7 1 27.4 24.8 21.3 12.4 15.7 12.7 12.3 10. I 10.5 14.4 8.8 13.0 12.1 10.6 10.9

-

-

20

0 -10

-20

30

26

26

24

22

20

I8

16

14

12

10

0

6

4

2

0

Y

2 4 6 8 10 12 14 16 I 8 5 X

Viscps$y Centtpotsu

f ::

By permission Irom HEAT TRANSMiSSION. by W. H. M c R d n m s Copyrighted 1954. McGraw.Hi11 Book Company, Inc.

m ua 0 n n r c U ua -.)


FIGURE P-5.4B

V I S C O S I T I E S OF G A S E S A N D V A P O R S m

A T a l b 0 0

3 8

1 A T M . w l n 0 0 0 0 d d


ION 8

FIGURE P-5.5

HIGH PRESSURE GAS VISCOSITY 10

8

6

5 5 3 > 1 4

d 0 I- -

3 >. t- (I) 0 0 E > 2

-

1.5

1 8 10 0.1 0.2 0.3 0.4 0.5 0.8 1 2 3 4 5 6

P REDUCED PRESSURE - P r =- P,

Reprinted by permission from Chemical Engineerina Progress Symposium Series. 51, No. 16, 1955. N. L. Carr. J. D. Parent. and R. E. Peck.

Substance

Acettc Acid Acetone Acetylene Acrylic Acid Ally1 Alcohol Ammonia Rniline Argoi. Benzene Bromobenzene 1.3 Butadiene n-Butane 3utylene Butyl Acetate n-Butyl Alcohol i-Butyl Alcohol Zorbon Dioxide Zarbon Disulhde Zarbon Monoxide Zarbon Tetrachloride Chlorine Chiorobenzene Chloroform Cumene Cyclohexane n-Decane Dichlorodifluoromethane Ethane Ethylene Ethyl Alcohol Ethyl Acetate Ethyl Benzene Fluorine Formaldehyde Helium

182

Molecular Weight

60 05 58 1 26 04 72 03 58 08 17 03 93 06 40 78 1

157 02 54 1 58 I 56 1

116 16 74 1 74 1 44 0 76 14 28 01

153 8 70 9

11256 1194 120 19 84 2

142 3 120 9 30 07 28 05 46 1 88 1

106 16 38 30 02 4 003

CRIl Critical

Temp.-Ti

1071 918 557

1176 982 730

1259 272

1013 1207 765 765 755

1043 1014 965 547 983 239

1001 751

1138 960

1136 998

1112 694 550 510 930 942

I l l 1 260 739

10

TABLE P6.1' CAL PROPERTY DATA

Substance :rrtical Pressure PSlA

840 694 890 734 83 1

1639 769 706 714 655 628 55 1 583 442 640 608

1070 1105 510 660

1119 655 805 467 588 304 597 708 730 925 557 536 808 984

n-Heptane Heptyl Alcohol n-Hexane Hexyl Alcohol Hydrogen Hydrogen Chloride Hydrogen Fluoride Hydrogen Iodide Hydrogen Sulfide Isobutane Isobutene Isopentane Krypton Methane Methyl Alcohol Methylethyl-Ketone Neon Nitrogen Nitrogen Oxide n-Nonane n-Octane Oxygen n-Pentane Phenol Propune Propylene n-Propyl Alcohol I-Propyl Alcohol Sulfolane Sulfur Dioxide Toluene Trichloroethylene Vinyl Acetate Vinyl Chloride

Molecular Weight

100 2 116 2 86 2

102 2 2 016

36 46 20 01

128 34 08 58 1 56 1 72 1 83 8 16 04 32 72 1 20 18 28 02 30 01

128 3 1142 32 72 I 94 1 44 1 42 1 60 1 60 1

120 2 64 1 92 1

131 4 86 1 62 5 18 02

Critical Temp -OR

972 1091

914 1055

60 584 830 763 672 735 752 830 376 343 926 964

80 227 325

1071 1025 278 846

1250 666 657 966 915

1442 775

1069 774 946

1028 1165

Jritical Pressure PSlA

397 436 440 490 188

1199 94 I

1191 1307 529 580 483 797 673

1174 603 395 492 950 332 362 737 490 890 617 667 750 69 1 767

1142 590 809 609 710

3206


GENERAL INFORMATION SECTION 9

CONTENTS

TABLE D-1 D-2 0-3 D-5 D-5M D-6 D-7 D-7M D-8 D-9 D-10 D-1OM D-1 1 D-1 1M D-12 D-12M D-13 D-14 D-15 D-16

TITLE PAGE Dimensions of Welded and Seamless Pipe ............................................................. Dimensions of Welded Fittings ................................................................................ Dimensions of ASME Standard Flanges .................................................................. Bolting Data - Recommended Minimum ................................................................. Metric Bolting Data - Recommended Minimum ...................................................... Pressure - Temperature Ratings for Valves, Fittings and Flanges .......................... Characteristics of Tubing ......................................................................................... Characteristics of Tubing (Metric) ............................................................................ Hardness Conversion Table ..................................................................................... Internal Working Pressures of Tubes At Various Values of Allowable Stress ........ Modulus of Elasticity ................................................................................................. Modulus of Elasticrty (Metric) ................................................................................... Mean Coefficients of Thermal Expansion ................................................................ Mean Coefficients of Thermal Expansion (Metric) .................................................. Thermal Conductivity of Metals ................................................................................ Thermal Conductivity of Metals (Metric) .................................................................. Weights of Circular Rings and Discs ........................................................................ Chord Lengths and Areas of Circular Segments ..................................................... Conversion Factors .................................................................................................. Conversion Tables for Wire and Sheet Metal Gages ..............................................

184 185 186-1 87 188 189 7 90-229 230 231 232 233-235 236 237 238 239 240 241 242-247 248 249-250 251


s 9

OMINAL 'IPE 'IZE

'/e '/a

3/8

'/i

3/4

-~

1

1% 1 %

2 2%

3

3%

4 5

6 8

10 12

140.D. 160.0.

180.D. 200.D.

22 O.D.

ION

NOMINAL WALL THICKNESS FOR OUT- 'IDE SCHED. SCHED. SCHED. SCHED. SCHED. STAND- SCHED. S C Z D . S:::$ SCHED. SCHED

0.405 0.049 0.068 0.068 0.095 0.095 0.540 0.065 0.088 0.088 0 119 0.119

0.675 0.065 0.091 0.091 0.126 0.126 0.840 0.065 0.083 0.109 0.109 0.147 0.147

1.050 0.065 0.083 0.113 0.113 0.154 0.154 1.315 0.065 0.109 0.133 0.133 0.179 0.179

1.660 0.065 0.109 0.140 0.140 0.191 0.191 1.900 0.065 0.109 0.145 0.145 0.200 0.200

2.375 0.065 0.109 0.154 0.154 0.218 0.218 2.875 0.083 0.120 0.203 0.203 0.276 0.276

3.5 0.083 0.120 0.216 0.216 0.300 0.300 4.0 0.083 0.120 0.226 0.226 0.318 0.318

4.5 0.083 0.120 0.237 0.237 0.337 0.337 5.563 0.109 0.134 0.258 0.258 0.375 0.375

6.625 0.109 0.134 0.280 0.280 0.432 0.432 8.625 0.109 0.148 0.250 0.277 0.322 0.322 0.406 0.500 0.500 0.594

10.75 0.134 0.165 0.250 0.307 0.365 0.365 0.500 0.500 0.594 0.719 12.75 0.156 0.180 0.250 0.330 0.375 0.406 0.562 0.500 0.688 0.844

14.0 0.156 0.188 0.250 0.312 0.375 0.375 0.438 0.594 0.500 0.750 0.938 16.0 0.165 0.188 0.250 0.312 0.375 0.375 0.500 0.656 0.500 0.844 '1.031

18.0 0.165 0.188 0.250 0.312 0.438 0.375 0.562 0.750 0.500 0.938 1.156 20.0 0.188 0.218 0.250 0.375 0.500 0.375 0.594 0.812 0.500 1.031 1.281

22.0 0.188 0.218 0.250 0.375 0.500 0.375 0.875 0 500 1.125 1.375

DIAM' 5s' 10s' 10 20 30 A R D t 40 § 80 100

-~--___~ - ~~

TABLE 0-1

DIMENSIONS OF WELDED AND SEAMLESS PIPE

1.OOO

1.094 1.219

1.375 1.500

1.625 1.812

1.125 1.312 1.OOO

1.250 1,406 1.438 1.594

1.562 1.781 1.750 1.969

1.875 2.125 2.062 2.344

SCHED. ~~ SCHED. SCHED.

'

34 O.D. 34.0 360.D. I 36.0

0.375

0.688

0.688 0.750 , 1

I I I 1

All dimensions are given in inches.

The decimal thicknesses listed for the respeGive pipe sizes represent their nominal or average wall dimensions. The actual thicknesses may be as much as 12.5% under t h e nominal thickness because of mi l l tolerance. Thicknesses shown in bold face are more readily available.

Schedules 5s and 10s are available in corrosion resistant materials and Schedule 10s is also available in carbon steel.

t Thicknesses shown in italics are available also in stainless steel, under the designation Schedule 40s.

5 Thicknesses shown in italics are available also in stainless steel. under the designation Schedule 80s.

Reprinted by permission of Tube Turns Division of Chemetmn Corporation


1% 1%

3'

~~~1 2

2 1% 1%

% 1

2% ...... ......

2% 2% 2% 2% 2% 2%

2% ...... 2% 2% 3 2% 2% 3 2% 2 3 2% 1% 3

2% 2% 2% j 2% 2% _,.... 2%

3 3 3 3 3

3% ...... ...... 3 3% 1 3%

2 3' & 1 3% ;g 2% 3%

1% 3% 1% 3% 2%

TABLE 0-2

DIMENSIONS OF WELDING FITTINGS (Ail Dimensions in inches)

Long Radius Weld Ells

m-: n - ~ --L+

Caps Stub Ends

Short Radius Weld Ells

Straiaht Tees Reducing Tees Con. & Ecc. Reducers

A D I L 1 Nom Pipe Size

1 1

- Size

16 16 16 16 16 16 16

4%

4% 3% 4%

:; I 3

...... ......

.~

9% -

4 .... 4 4 4 4 4

11 11 11 11 11

12 - --

3%

2% 3

2 1 Y4 I 1);

I 1%

1%

~~ ......

4% 4% 2% 4% 4%

4% 4% 5 S

...... ...... 12 14 11% 14 11% 14 10% 14 10% 14

12 12 12 12 12

3 ' - I 5% 4% s2 6 6 I 2% I 5% I 4% I 5%

...... ......

~~

2% 2% 3%

I x I ; ...... ......

6% 7 I S I 4 I 7

j 3 % \ 7 20 20 1s 24 24 17 ...... ... ..

10 10 10 10 10

i 1;

i ; I

4

...... ...~_. 8 7 7% 7 7% 7 7% 7

I I 1 1 I Reprinted by permiasion of Taylor Forge & Pipe Work.

Standards Of The Tubular lExchanger Manufacturers Association 185

SECTION 9

N0m.

Size pip.

% %

1% 1%

2%

3%

1

2

3

4

5 6 8

10 12

14 16 18 20 24

GENERAL INFORMATION

A

3% 3% 4% 4% 5

6 7 7% 8% 9

10 11 13% 16 19

21

25 27% 32

23%

TABLE D-3

DIMENSIONS OF ASME STANDARD FLANGES (All Dimensions in Inches)

WELDING NECK FLANGE THREADED FLANGE SLIP ON FLANGE

& , ? j = j j @ + +A-

A

3%

4% 5%

4%

6%

6% 7% 8%

10% 9

13 14 16% 20 22

23?4 27

32 37

29%

TO

%b

’%6 %b

%

% 1 1% 1% 1% 1%

1% 1% 2% 2% 2%

2% 3 3% 3% 4

Neld Neck

2%‘ 2%

2% 23;

2% 3%

3%

4% 4% 5%

2%b

3%

4

6 6%

6% 7 7% 7% 8

Thrd. Slip on

%

1% 1%

1% 1%

1% 2%

2% 2%

1 1%b

1’Xb

3 3% 3%

3% 4x6 1%

5% 5

%

1X6 1% 1%

1 % 2% 4% % 3% 4%

3% 4% 3% 47% 1% 4% 4 4 1%

1

LAP JOINT FLANGE BUND FLANGE

150 LB. FLANGES 300 LB. FLANGES

A No. and

Holes

3% 4% 4% 5% 6%

65; 7 !4 8%

~

9 10

4-%

8-%

11

15 17%

23

28 30% 36

12%

20%

25%

__.

~

8% 12-% 12-1 16-1% 16~1%

20-1% 16

24-1% i 24 24.1% 20 24-1%

20.1%

12-1 1 - 1

2% 1 5 % I 3

1 6 - 1 3 2 I

400 LB. FLANGES 600 LB. FLANGES I I I

__.

Lap joinf

:ircle Bolt 1 No’ S ize and of Holes

No . and

loin1

Nom. Pipe Size

% %

1% 1%

2%

3%

1

2

3

4

5 6 8

10 12

14 16 18 20 24

f 4-%

8% 8% 8% 8-1

7% 8-1

2% 2%

4 %

2‘%b 4

1% I 1;:; 12.1% 16.1%

4%

5% 5%

5

6% - 24-1 %

Reprinled by permission of Taylor Forge & Pipe Works


Bolt Circle

3% 3%

4% 4 4%

6% 7% 8 _.,_.. 9%

11% 12% 15;4 19 22%

25 27% 30% 323; 39

No. and

y~,‘ 4-% 4-%

4-1 4-1 4-1%

8-1 8-15, 8.1%

8-136

8 1% 12.1% 12.1% 12-2 162%

16-2?/, 16-23’s 16.2% 16-3% 16.3%

. ....

LO Thrd.

s l ip on

1% 1% 1% 1% 1%

2% 2% 2% ..___. 3x4

4%

5% 6% 7%

4’Xb

......

......

......

..,...

.,....

Lap Joint

15; 1% 1% 1% 1%

2% 2% 2% .... .. 3%6

4%

5% 7 8%

9% 10% 10% 11%

4’Kb

13

Nom Pipe Outside Sched Sched Sched Standard Sched Sched Extra Size Diameter 10 20 30 Wall 40 60 Strong

lfz 0 840 0 622 0 622 0 546 ’A 1050 0 824 0 824 0 742

I 049 1049 0 957 1 1312 1% 1 660 I 380 1 380 1278

1 610 1610 1500 2 067 2 067 1939 2

2% 2 875 2 469 2 469 2 323 3 3 500 3 068 3 068 2 900 3% 4 000 3 548 3 548 3 364

4 026 4 026 3 826 4 4 500 5 S 563 5 047 5 047 4 813 6 6 625 6 065 6 065 5 761 8 8 625 8 125 8071 7 981 7 981 7 813 7 625 10 10 750 10 250 10 136 10 020 10 020 9 750 9 750 12 12 750 12250 12090 12 000 1 1 938 11 626 1 1 750 14 14 000 13 500 13 375 13 250 13 250 13 124 12 814 13 000 16 16 000 15 500 15 375 IS 250 15 250 15 000 14 688 15 000 18 18 000 17500 17 375 17 124 17 250 16 876 16500 17 000 20 20 000 19 500 19 250 19 000 19 250 18 814 18 376 19 000 24 24 000 23 SO0 23 250 22 876 23 250 22 626 22 064 23 000

1% ; y&

30 30 000 29 376 29 000 28 750 29 250 29 000

Sched 80

0 546 0 742 0 957 1278 1500 1939 2323 2 900 3 364 3 826 4 813 5 761 7625 9 564

1 1 376 12500 14 314 16 126 17 938 21 564

TABLE D3-(Continued)

DIMENSIONS OF ASME STANDARD FLANGES

900 LB. FLANGES 1500 LB. FLANGES N o m Pipe Size

N o . and Size of Holes A ___

Weld Neck

Weld Neck

1,;

1% 1%

Wl 3);

k 1

- 2

3

4

23, 2 314 2 5 8

3 /4

4 4!€ 4

4 ‘ 2

2 F

I___

4-% 4 .h 4- 1 4-1 4-1:s

4 % 5% 5% 6% 7

8 92 9 K

lOV?

12’4

__

%

1% 1% 1%

1% 1% 1%

2 Ye

1

-

......

2% 2% 2% 2% 3%

5 ts

2 8 52 2’2 93s

3‘ I 4 1152

5 13% 6 15

3 9’2

-

8 18% 10 2155 12 24

8-1

8-1 8-1!8

8-11.,

4 4% 4%

4%

6% 6% 8%

11%

......

~

10

8-lYi 12-1% 12-1%

20-1 I/; 16-1%

5 6 8

10 12

5 5’ i 6? B

7 % 7 !d

14% 15% 19 23 26 % 29!4 32% 36 38% 46

-

2% 3% 3% 4% 4%

14 16 18 20 24

8 !.a 8! 2

9% l l ? ,

9

5% 5% 6% 7 8

11% 12% 12% 14 16 -

20.1% 20.1% 20-2 20-2’/;1 20-2%

5% 65s 22 5% 6% 24!4

6% 29% 6 7 )~ ; 27

8 10% 35%

Yo. and Size of Hole.

(1) Bore to match schedule of attached pipe.

(2) Includes 1/16” raised face in 150 pound and 300 pound standard. Does not include raised face in 400, 600, 900, 1500 and 2500 pound standard.

(3) Inside pipe diameiers are also provided by this table.

N o m Pipe Size

1 , I

%

1% 1 !4

1

4. % 4. % 4-1 4-1 % 4.1);

2

3 4 5

2% 8.1%

8-1 % 8.1% 8.1%

12.2%

8.1%

8-2% 6 8

10 12

Reprinted by permission of Taylor Forge & Pipe Works

I I


TABLE D-5

BOLTING DATA - RECOMMENDED MINIMUM (All Dimensions in Inches Unless Noted)

1%

1%

1%

1%

1 Threads I NutDin

8

8

8

8

tensions Wrench Bolt ~ Bolt Radial Radial Edge Diam- Bolt

Root Across Across Spacing Distance Distance Distance eter Size Area in.? Fiats Corners B R h R. E a dB

, 1

0.728

0.929

1% 2% 1% 1'%6 2.002 2% 1% 1%

2 2.209 2'%6 1%. 1% 1% 1 3% 1%

0.202 l % 6 1.175 1% '%6 % % 1% %

0.302 1% 1.383 1% 1% "A6 ' % 6 2 x 6 %

1%6 ' % 6 "A6 2% % 1.589 2 x 6 1% 0.419

0.551 1% 1.796 2% 1%

I f

1% 8 1.680 2% 2.828 3% 2% 1% 4 1%

1% 4% 1% 1% 8 1.980 2% 3.035 3% 2%

1% 4% 1% 1% 8 2.304 2% 3.242 4 2%

2 4% 2 2 8 2.652 3% 3.449 4% 2%

2% 5% 2% 2% 8 3.423 3% 3.862 4% 2%

2% 5% 2%

2% 6% 2%

2% 8 4.292 3% 4.275 5% 31/16

2% 8 5.259 4% 4.688 5% 3%

3 8 6.324 4% 5.102 6% 3% 2% 7 3

I 3% I 8 I 7.487 I 5 I 5.515 I 6% I 3% I 1 3 7 % 1 3 % 1

3%

3%

4 I

I I I I I I I I

1% I 3% I 1% 1.155 I 2%6 I 2.416 I 3 x 6 I 1% I 1% I

8 8.149 5% 5.928 7% 4% 3% 8 3%

3% 8% 3% 8 10.108 5% 6.341 1% 4 ' h

8 11.566 6% 6.755 8% 4% 3% 9 4

I I

188

Nut dimensions are based on American National Standard B18.2.2 Threads are National Coarse series below 1 inch and eight-pltch thread series 1 inch and above


GENERAL I ~ F ~ R M A ~ I O ~

Threads Nut Dimensions

Pitch Roof ea Across Hats Across Bolt Radial Radial Edge Corners Spacing Distance Distance Dlstance

8 Rh Rr E 3 Bolt Size

dB (mm 1

M12 175 72 398 21 00 24 25 31 75 20 64 15 88 15 88

M16 200 138 324 27 00 31 18 44 45 28 58 20 64 20 64

M20 250 217 051 34 00 39 26 52 39 31 75 23 81 23 81

M22 250 272 419 36.00 41 57 5398 33 34 25 40 25 40

M24 3 00 312 748 41 00 47 34 58 74 36.51 28 58 28 58 M27 300 413.852 46 00 53 12 63 50 38 10 29 00 29 00

M30 350 502 965 50 00 57 74 73 03 46 04 33 34 33 34

M36 4 00 738 015 60 00 69 28 84 14 53 97 39 69 39 69

M42 450 1018 218 70 00 80 83 100 00 61 91 49 21

M48 500 7342959 8000 92 38 11271 68.26 55 56

M56 550 1862725 9000 103.92 127 00 76 20 63 50

M64 600 2467150 10000 11547 139 70 84 14 66 68

M72 600 3221775 11000 127.02 155.58 88.90 69 85

M80 6 00 4076.831 120.00 138.56 166.69 93.66 74 61

M90 600 5287 085 135.00 155.88 188.91 107.95 84 14

MlOO 600 6651 528 150.00 173.21 207 96 11906 93 66 ----

TABLE D-5M

,

Bolt Size dB

m12 M16

M20 M22

M24

M27

M30

M36

M42

M48

M56

M64

M72

M80

M90

MlOO


SECTION 9 GENERAL INFORMATION

D-6 TABLES FOR

FOR VALVES, FITTINGS, AND FLANGES INTRODUCTORY NOTES

PRESSURE-TEMPERATURE RATINGS

1. Products used within the jurisdiction of the ASME Boiler and Pressure Vessel Code and the ASME Standard for pressure piping are subject to the maximum temperature and stress limitations upon the material and piping stated therein.

2. The ratings at -20 O F to 100 O F, given for the materials covered on pages 194 to 229 inclusive, shall also apply at lower temperatures. The ratings for low temperature service of the cast and forged materials listed in ASTM A352 and A350 shall be taken the same as the -20 O F to 100 O F ratings for carbon steel on pages 194 to 229 inclusive.

resistance at temperatures lower than -20 F to such an extent as to be unable to safely resist shock loadings, sudden changes of stress or high stress concentrations. Therefore, products that are to operate at temperatures below -20 O F shall conform to the rules of the applicable Codes under which they are to be used.

3. The pressure-temperature ratings in the tables apply to all products covered by this ASME Standard. Valves conforming to the requirements of this ASME Standard must, in other respects, merit these ratings.

All ratings are the maximum allowable nonshock pressures (psig) at the tabulated temperature (degrees F) and may be interpolated between the temperatures shown. The primary service pressure ratings (1 50, 300, 400,600, 900, 1500, 2500) are those at the head of the tables and shown in bold face type in the body of the tables.

Temperatures (degrees F) shown in the tables, used in determining these rating tables, were temperatures on the inside of the pressure retaining structure.

The use of these ratings require gaskets conforming to the requirements of Paragraph 5.4 of ASME B16.5-(1996). The user is responsible for selecting gaskets of dimensions and materials to withstand the required bolt loading without injurious crushing, and suitable for the service conditions in all other respects. Reference: American Society of Mechanical En ineers Standard Steel Pipe Flanges and Flanged Fittings (ASME Standard B16.5-(1996 and 19987) reprinted with the permission of The American Society of Mechanical Engineers, United Engineering Center, 345 E. 47th Street, New York, NY 10017. All rights reserved.

Some of the materials listed in the rating tables undergo a decrease in impact


GENERAL INF

TABLE ?A LIST OF MAnRlAL SPECIFICATIONS

Material Group

1.1

1.2

1.3

1.4

1.5

1.7

1.9

1.10

1.13

I I Pressure- I Applicable ASTM Specifications’ .. Nominal Temperature

Designation Rating Table Forgings Castings

C-Si 2-1.1 A 105 A 216 Gr. WCB C-Mn-Si A 350 Gr. LF2

C-Mn-Si-V

C-Mn-Si 2-1.2 A 216 Gr. WCC A 352 Gr. LCC

C-Mn-Si-V 2’/2Ni A 352 Gr. LC2 3’/2Ni A 350 Gr. LF3 A 352 Gr. LC3

C-Si 2-1.3 A 352 Gr. LCB C-Mn-Si 2%Ni 3’4Ni

A 350 Gr. LF6 CI. 1

A 350 Gr. LF6 CI. 2

C-Si 2-1.4 C-Mn-Si

C-Y~MO 2-1.5 A 182 Gr. F1 A 217 Gr. WC1

A 350 Gr. LFl CI. 1

A 352 Gr. LC1

C-‘/zMo 2- 1.7 ’/ZCr- Y2Mo Ni-l/2Cr-l/~Mo A 217 Gr. WC4 3/4Ni-3/&r-1M~ A 217 Gr. WC5

1Cr-YzMo 2- 1.9 A 182 Gr. F12 CI. 2 174Cr-YzMo A 217 Gr. WC6 1 %Cr-’/zMo-Si A 182 Gr. F l l CI. 2

2%Cr- 1 Mo 2-1.10 A 182 Gr. F22 CI. 3 A 217 Gr. WC9

5Cr-YzMo 2-1.13 A 182 Gr. F5

A 182 Gr. F2

A 182 Gr. F5a A 217 Gr. C5

1.15

2.1

2.2

1.14 I 9Cr-1Mo

9Cr-1 Mo-V 2-1.15 A 182 Gr. F91 A 217 Gr. Cl2A

18Cr-8Ni 2-2.1 A 182 Gr. F304 A 351 Gr. CF3 A 351 Gr. CF8 A 182 Gr. F304H

16Cr-12Ni-2Mo 2-2.2 A 182 Gr. F316 A 351 Gr. CF3M A 351 Gr. CF8M

18Cr-13Ni-3Mo 1SCr-l ONi-BMo A 351 Gr. CG8M

A 182 Gr. F316H

I 2-1.14- I A 182 Gr. F9 1 A 217 Gr. C12

2.3

2.4

~

18Cr-8Ni 2-2.3 A 182 Gr. F304L 16Cr-12Ni-2Mo A 182 Gr. F316L

18Cr-1ONi-Ti 2-2.4 A 182 Gr. F321 A 182 Gr. F321H

Plates

A 515 Gr. 70 A 516 Gr. 70 A 537 CI. 1

A 203 Gr. B A 203 Gr. E

A 515 Gr. 65 A 516 Gr. 65 A 203 Gr. A A 203 Gr. D

A 515 Gr. 60 A 516 Gr. 60

A 204 Gr. A A 204 Gr. B

A 204 Gr. C

A 387 Gr. 11 CI. 2

A 387 Gr. 22 CI. 2

A 387 Gr. 91 CI. 2

A 240 Gr. 304 A 240 Gr. 304H

A 240 Gr. 316 A 240 Gr. 316H A 240 Gr. 317

A 240 Gr. 304L A 240 Gr. 316L

A 240 Gr. 321 A 240 Gr. 321H

Reprinted from ASME B16.5-1996 and 1998, by permission of The American Society of Mechanical Engineers. All rights reserved


N

TABLE 1A

Material Nominal Group Designation

2.5 18Cr-1ONi-Cb

2.6 25Cr-12Ni

230-12Ni

2.7 250-20Ni

2.8 20Cr-18Ni-6Mo 220-5Ni-3Mo-N 25Cr-7Ni-4Mo-N 240-10Ni-4Mo-V 25Cr-5Ni-ZMo-3Cu 25Cr-7Ni-3.5Mo-W-Cb

25Cr-7Ni-3.5Mo-N-Cu-W

3.1 35Ni-35Fe-20Cr-Cb

3.2 99.ONi

3.3 99.ONi-Low C

3.4 67Ni-30Cu 67Ni-30Cu-S

3.5 72Ni- 15Cr-8Fe

3.6 33Ni-42Fe-21Cr

3.7 65Ni-28Mo-2Fe

3.8 54Ni- 16Mo- 15Cr 6ONi-22Cr-SMo-3.5Cb 62Ni-28Mo-5Fe 70Ni-16Mo-7Cr-5Fe 61Ni- 16Mo- 16Cr 42Ni-21.5Cr-3Mo-2.3Cu

3.9 47Ni-22Cr-SM0-18Fe

3.10 25Ni-46Fe-21Cr-5Mo

3.1 1 44Fe-25Ni-21Cr-Mo

3.12 26Ni-43Fe-22Cr-5Mo 47Ni-22Cr-20Fe-7Mo

LIST OF MATERIAL SPECIFICATIONS (CONT'D) Pressure- Applicable ASTM Specifications'

Temperature Rating Table Forgings Castings Plates

2-2.5 A 182 Gr. F347 A 351 Gr. CF8C A 240 Gr. 347 A 240 Gr. 347H A 240 Gr. 348 A 240 Gr. 348H

A 182 Gr. F347H A 182 Gr. F348 A 182 Gr. F348H

2-2.6 A 351 Gr. CH8 A 351 Gr. CH2O

A 240 Gr. 309s A 240 Gr. 309H

2-2.7 A 182 Gr. F310 A 351 Gr. CKZO A 240 Gr. 310s A 240 Gr. 310H

2-2.8 A 182 Gr. F44 A 351 Gr. CK3MCuN A 240 Gr. 531254 A 240 Gr. S31803 A 240 Gr. S32750

A 182 Gr. F51 A 182 Gr. F53

A 351 Gr. CE8MN A 351 Gr. CD4MCu A 351 Gr.

CD3MWCuN A 182 Gr. F55 A 240 Gr. S32760

2-3.1 B 462 Gr. NO8020 B 463 Gr. NO8020

2-3.2 B 160 Gr. NO2200 B 162 Gr. NO2200

2-3.3 B 160 Gr. NO2201 B 162 Gr. NO2201

2-3.4 B 564 Gr. NO4400 B 127 Gr. NO4400 B 164 Gr. NO4405

2-3.5 B 564 Gr. NO6600 B 168 Gr. NO6600

2-3.6 B 564 Gr. NO8800 B 409 Gr. NO8800

2-3.7 B 335 Gr. N10665 B 333 Gr. N10665

2-3.8 B 564 Gr. N10276 B 575 Gr. N10276 B 443 Gr. NO6625 B 333 Gr. N10001 B 434 Gr. N10003 B 575 Gr. NO6455 B 424 Gr. NO8825

2-3.9 B 572 Gr. NO6002 B 435 Gr. NO6002

2-3.10 B 672 Gr. NO8700 B 599 Gr. NO8700

2-3.1 1 B 649 Gr. NO8904 B 625 Gr. NO8904

2-3.12 B 621 Gr. NO8320 B 620 Gr. NO8320 B 582 Gr. NO6985

B 564 Gr. NO6625 B 335 Gr. NlOOOl B 573 Gr. N10003 B 574 Gr. NO6455 B 564 Gr. NO8825

B 581 Gr. NO6985

(Table 7A continues on next page; Notes follow at end of Table)

Reprinted from ASME B16.51996 and 1998, by permission of The American Society of Mechanical Engineers. All rights resewed


GENERAL INFORMATION

Material Group

3.13

3.14

3.15

3.16

3.17

SECTION 9

Pressure- Applicable ASTM Specifications' Nominal Temperature

Designqtion Rating Table Forgings Castings Plates

B 582 Gr. NO6975 49Ni-25Cr-lBFe-6Mo 2-3.13 B 581 Gr. NO6975 B 625 Gr. NO8031 Ni-Fe-Cr-Mo-Low Cu B 564 Gr. NO8031

47Ni-22Cr-19Fe-6Mo 2-3.14 B 581 Gr. NO6007 B 582 Gr. NO6007

B 564 Gr. NO8810 B 409 Gr. NO8810

35Ni-19Cr-l%Si 2-3.16 B 511 Gr. NO8330 B 536 Gr. NO8330

29Ni-20.5Cr-3.5Cu-2.5Mo 2-3.17 A 351 Gr. CN7M

33Ni-42Fe-21 Cr 2-3.15

TABLE 1A LIST OF MAERIAL SPECIFICATIONS ICONT'D)

hpfinted from ASME B16.51996 and 1998, by permission of The American Society of Mechanical Engineers. All rights resewed


SECTION 9

Nominal Designation Forgings Castings

C-Si A 105 (1) A 216 Gr. WCB (1)

GENERAL INFORMATION

Plates

A 515 Gr. 70 (1)

TABLES 2

GROUPS 1.1 THROUGH 3.17 MATERIALS PRESSURE-TEMPERATURE RATINGS FOR

C-Mn-Si A 350 Gr. LF2 (1)

C-Mn-Si-V

A 516 Gr. 70 (1)(2) A 537 CI. 1 (3)

A 350 Gr. LF6 CI. 1 (4)

Class Temp.. O F

WORKING PRESSURES BY CLASSES.

150

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000

285 260 230 200 170

140 125 110 95 80

65 50 35 20

300

740 67 5 655 635 600

550 535 535 505 410

270 170 105 50

194

400

990 900 875 845 800

730 715 710 670 550

355 230 140 70

600

1480 1350 1315 1270 1200

1095 1075 1065 1010 825

535 345 205 105

J g

900

2220 2025 1970 1900 1795

1640 1610 1600 1510 1235

805 515 310 155

1500 I 2500

3705 3375 3280 3170 2995

2735 2685 2665 2520 2060

1340 860 515 260

6170 5625 547 0 5280 4990

4560 4475 4440 4200 3430

2230 1430 860 430

Reprinted from ASME 816.51996 and 1998, by permission of The American Society of Mechanical Engineers. All rights resewed


N

Nominal Designation

C-Mn-Si

C-Mn-Si-V

2%Ni

3%Ni

TABLE 2-1.2 RATINGS FOR GROUP 1.2 MATERIALS

Forgings Castings

A 216 Gr. WCC (1) A 352 Gr. LCC (2)

A 350 Gr. LF6 CI. 2 (3)

A 352 Gr. LC2

A 352 Gr. LC3 A 350 Gr. LF3

Class Temp., 'F

-20 to 100 200 300 400 500

A 203 Gr. B (1)

A 203 Gr. E (1)

150

290 260 230 200 170

(1) Upon prolonged exposure to temperatures above 80O0F, the carbide phase of steel may be converted to graphite. Permissible, but not recommended for prolonged use above 800°F.

(2) Not to be used over 650°F. (3) Not to be used over 500°F.

140 125 110 95 80

WORKING PRESSURES

605 590 570 505 410

300

750 750 730 705 665

600 650 700 750 800

400

1000 1000 970 940 885

805 785 755 670 550

355 230 140 70

3Y CLASSES. psig

MI0

1500 1500 1455 1410 1330

1210 1175 1135 1010 825

535 345 205 105

900

2250 2250 2185 21 15 1995

1815 1765 1705 1510 1235

805 515 310 155

1500

3750 3750 3640 3530 3325

3025 2940 2840 2520 2060

1340 860 515 260

2500

6250 6250 6070 5880 5540

5040 4905 4730 4200 3430

2230 1430 860 430

Reprinted from ASME 816.5-1996 and 1998, by permission of The American Society of Mechanical Engineers. All rights reserved


SECTION 9


C-Si

C-Mn-Si

A 352 Gr. LCB (3)

GENERAL INFORMATION

Plates

A 515 Gr. 65 (1)

A 516 Gr. 65 (1")

3YzNi I 2v2Ni

1 A 203 Gr. D (1) I A 203 Gr. A ( l )

NOTES: (1) Upon prolonged exposure to temperatures above 800°F, the carbide phase of steel may be

converted to graphite. Permissible, but not recommended for prolonged use above 800°F. (2) Not to be used over 850°F. (3) Not to be used over 650°F.

Class Temp., OF

-20 to 100 200 300 400 500

600 650 700 750 aoo

a50 900 950

1000

196

150

265 250 230 200 170

140 125 110 95 ao

65 50 35 20

WORKING PRESSURES BY CLASSES, psig

300

695 655 640 620 585

535 525 520 475 390

270 170 105 50

400

925 a75 a50 825 775

710 695 690 630 520

355 230 140 70

600

1390 1315 1275 1235 1165

1065 1045 1035 945 780

535 345 205 105

900

2085

i a50

1970 1915

1745

1600 1570 1555 1420 1175

a05 515 310 155

1500

3470

3190

2910

2665 2615 2590 2365 1955

1340

515 260

3280

3085

a60

Reprinted from ASME 816.51996 and 1998, by permission of The American Society of Mechanical Engineers. All rights reserved

2500

5785 5470 5315 5145 4850

4440 4355 4320 3945 3260

2230 1430 860 430


GENERAL INF


C-Si

C-Mn-Si A 350 Gr. LF1, CI. 1 (1)

SE

Plates

A 515 Gr. 60 (1)

A 516 Gr. 60 (1)(2)

400

825 750 730 705 665

610 600 600 590 495

355 230 140 70

- - - -

NOTES: (1) Upon prolonged exposure to temperatures above 800"F, the carbide phase of steel may be

converted to graphite. Permissible, but not recommended for prolonged use above 800°F. (2) Not to be used over 850°F.

600 900 1500

1235 1850 3085 1125 1685 2810 1095 1640 2735 1060 1585 2645 995 1495 2490

915 1370 2285 895 1345 2245 895 1345 2245 885 1325 2210

. 740 1110 1850

535 805 1340 345 515 860 205 310 515 105 155 260

Class Temp., 'F

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950 1000

150

235 215 210 200 170

140 125 110 95 80

65 50 35 20

WORKING PRESSURES BY CLASSES. nsis

300

620 560 550 530 500

455 450 450 445 370

270 170 105 50


2500

5145 4680 4560 4405 41 50

3805 3740 3740 3685 3085

2230 1430 860 430

Standards Of The Tubular Exchanger Manufacturers Association I97

SECTION 9 GENERAL IN FORMATION


C-Y~MO A 182 Gr. F1 (1) A 217 Gr. WC1 (1)(2) A 352 Gr. LC1 (3)

Plates

A 204 Gr. A (1) A 204 Gr. B (1)

Class Temp., OF

-20 to 100 200 300 400 500

1500

3470 3395 3260 3200 3105

3025 2940 2840 2660 2540

2435 2245 1405 825

600 650 700 750 800

2500

5785 5660 5435 5330 5180

5040 4905 4730 4430 4230

4060 3745 2345 1370

850 900 950 1000

198

150

265 260 230 200 170

140 125 110 95 80

65 50 35 20

WORWI

300

695 680 655 640 620

605 590 570 530 510

485 450 280 165

i PRESSURE

400

925 905 870 855 830

805 785 755 710 675

650 600 375 220

BY CLASSES,

600

1390 1360 1305 1280 1245

1210 1175 1135 1065 1015

975 900 560 330

isig

900

2085 2035 1955 1920 1865

1815 1765 1705 1595 1525

1460 1350 845 495

-I



GENERAL INFQR


C-'/~MO

'/zCr-YZMo

N i - '/&r - V2Mo

3/4Ni-3/4Cr- 1 Mo

A 182 Gr. F2 (3)

A 217 Gr. WC4 (2)(3)

A 217 Gr. WC5 (2)

Plates

A 204 Gr. C (1)

Class Temp., 'F

-

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

150

290 260 230 200 170

140 125 110 95 80

65 50 35 20 . . .


300

750 750 720 695 665

605 590 570 530 510

485 450 315 200 1 60

400

1000 1000 965 925 885

805 785 755 710 675

650 600 420 270 210

600

1500 1500 7445 1385 1330

1210 1175 1135 1065 1015

975 900 630 405 315

900

2250 2250 2165 2080 1995

1815 1765 1705 1595 1525

1460 1350 945 605 47 5

1500

3750 3750 3610 3465 3325

3025 2940 2840 2660 2540

2435 2245 1575 1010 790



2500

6250 6250 6015 5775 5540

5040 4905 4730 4430 4230

4060 3745 2630 1685 1315

199

SECTION 9

Nominal Designation Forgings

lCr-'/2Mo

1 v4Cr - v2M o

A 182 Gr. F12 CI. 2 (1)(2)

GENERAL INFORMATION

Castings Plates

A 217 Gr. WC6 (1)(3)

l'/,Cr-'/zMo I A 182 Gr. F11 CI. 2 (1)(2) I 1 A 387 Gr. 11 CI. 2 (2)

NOTES: (1) Use normalized and tempered material only. (2) Permissible, but not recommended for prolonged use above 1100°F. (3) Not to be used over 1100°F.

WORKII

Class Temp., "F

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200

200

150

290 260 230 200 170

140 125 110 95 80

65 50 35 20

. . *

. . .

...

. . .

300

750 750 720 695 665

605 590 570 530 510

485 450 320 215 145

95 60 40

j PRESSURES BY CLASSES, psig

400

1000 1000 965 925 885

805 785 755 710 675

650 600 425 290 190

130 80 50

600

1500 1500 1445 1385 1330

1210 1175 1135 1065 1015

975 900 640 430 290

190 125 75

900

2250 2250 2165 2080 1995

1815 1765 1705 1595 1525

1460 1350 955 650 430

290 185 115

1500

3750 3750 3610 3465 3325

3025 2940 2840 2660 2540

2435 2245 1595 1080 720

480 310 190

2500

6250 6250 6015 5775 5540

5040 4905 4730 4430 4230

4060 3745 2655 1800 1200

800 51 5 315

Reprinted from ASME B16.51996 and 1998, by permission of The American Society of Mechanical Engineers. All rights reserved


GENERAL INFORMATION


Z'/&r-lMo A 182 Gr. F22 CI. 3 (2)

SECTION 9

Castings Plates

A 217 Gr. WC9 (1)(3) A 387 Gr. 22 CI. 2 (2)

Class Temp., "F

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200

150

290 260 230 200 170

140 125 110 95 80

65 50 35 20 . . .

. . .

. . .

. . .

WORKING PRESSURES BY CLASSES,

300

750 750 730 705 665

605 590 570 530 510

485 450 375 260 175

110 70 40

400

1000 1000 970 940 885

805 785 755 710 675

650 600 505 345 235

145 90 55

600

1500 1500 1455 1410 1330

1210 1175 1135 1065 1015

975 900 755 520 350

220 135 80

sig

900

2250 2250 2185 2715 1995

1815 1765 1705 1595 1525

1460 1350 1130 780 525

330 205 7 25

1500

3750 3750 3640 3530 3325

3025 2940 2840 2660 2540

2435 2245 1885 1305 875

550 345 205


2500

6250 6250 6070 5880 5540

5040 4905 4730 4430 4230

4060 3745 3145 2170 1455

975 570 345


SECTION 9

Nominal Designation

5Cr-?iMo

GENERAL ~NFORMATION

Forgings Castings Plates

A 182 Gr. F5 A 182 Gr. F5a A 217 Gr. C5 (1)


Class Temp., "F

-20 to 100 200 300 400 500

600 650 700 750 800

a50 900 950

1000 1050

1100 1150 1200

202

150

290 260 230 200 170

140 125 110 95 ao

65 50 35 20 . . .

. . . * . .

. . .


300

750 745 715 705 665

605 590 570 530 510

485 370 275 200 145

I00 60 35

400

1000 995 955 940 885

a05 785 755 705 675

645 495 365 265 190

135

45 ao

600

1500 1490 1430 1410 1330

1210 1175 1135 1055 1015

965 740 550 400 290

200 125 70

;is

900

2250 2235 2150 2115 1995

1815

1585

1765 1705

1525

1450 1110

595 430

300

105

825

185

1500

3750 3725

3530 3325

3025 2940

2640 2540

2415

1370 995 720

495 310 170

3580

2840

1 a50

2500

6250 6205 5965

5540

5040 4905 4730 4400 4230

4030

5880

3085 2285 1655 1200

a30 515 285



GENERAL INFORMATION


9Cr- 1Mo A 182 Gr. F9 A 217 Gr. C72 (1)

SECTION 9

Plates

Class Temp., "F

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950 1000 1050

1100 1150 1200

150

290 260 230 200 170

140 125 110 95 80

65 50 35 20 . . .

. . .

. . .

. . .


300

750 750 730 705 665

605 590 570 530 510

485 450 375 255 170

115 75 50

400

1000 1000 970 940 885

805 785 755 710 675

650 600 505 340 230

150 100 70

600

1500 1500 1455 1410 1330

1210 1175 1135 1065 1015

975 900 755 505 345

225 150 105

900

2250 2250 2185 2115 1995

1815 1765 1705 1595 1525

1460 1350 1130 760 515

340 225 155

1500

3750 3750 3640 3530 3325

3025 2940 2840 2660 2540

2435 2245 1885 1270 855

565 375 255


2500

6250 6250 6070 5880 5540

5040 4905 4730 4430 4230

4060 3745 3145 2115 1430

945 630 430


N

Nominal I Designation Forgings

9Cr-1Mo-V A 182 Gr. F91


Castings Plates

A 217 Gr. C12A A 387 Gr. 91 CI. 2

Class Temp., 'F

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200

WORKING PRESSURES BY CUSSES. psig

150 300 400 600 900 1500

290 750 1000 1500 2250 3750 260 750 1000 1500 2250 3750 230 730 970 1455 2185 3640 200 705 940 1410 2115 3530 170 665 885 1330 1995 3325

140 605 805 1210 1815 3025 125 590 785 1175 1765 2940 110 570 755 1135 1705 2840 95 530 710 1065 1595 2660 80 510 675 1015 1525 2540

65 485 650 975 1460 2435 50 450 600 900 1350 2245 35 385 515 775 1160 1930 20 365 485 725 1090 1820 . . . 360 480 720 1080 1800

... 300 400 605 905 1510

. . . 225 295 445 670 1115

... 145 190 290 430 720


2500

6250 6250 6070 5880 5540

5040 4905 4730 4430 4230

4060 3745 3220 3030 3000

2515 1855 1200


AL INF N

Nominal Designation

18Cr-8Ni



A 351 Gr. CF3 12)

A 351 Gr. CF8 (1)

A 240 Gr. 304 (1)

A 240 Gr. 304H

A 182 Gr. F304 (1)

A 182 Gr. F304H

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200 1250 1300

1350 1400 1450 1500

150

275 230 205 190 170

140 125 110 95 80

65 50 35 20 ... ... . . . . . . . . . ... ... ... ... . . .

WORKING PRESSURES BY CLASSES

300

720 600 540 495 465

435 430 425 41 5 405

395 390 380 320 310

255 200 155 115 85

60 50 35 25

400

960 800 720 660 620

580 575 565 555 540

530 520 510 430 410

345 265 205 150 115

80 65 45 35

600

1440 1200 1080 995 930

875 860 850 830 805

790 780 765 640 615

51 5 400 310 225 170

125 90 70 55

aig

900

2160 1800 1620 1490 1395

1310 1290 1275 1245 1210

1190 1165 1145 965 925

770 595 465 340 255

185 145 105 80

1500

3600 3000 2700 2485 2330

2185 2150 2125 2075 2015

1980 1945 1910 1605 1545

1285 995 770 565 430

310 240 170 135

2500

6000 5000 4500 4140 3880

3640 3580 3540 3460 3360

3300 3240 3180 2675 2570

2145 1655 1285 945 715

515 400 285 230

Reprinted from ASME B16.51996 and 1998, by permission of The American Society of Mechanical Engineers. All rights reserved


SECTION 9

Nominal Designation

16Cr-12Ni-2Mo


A 351 Gr. CF3M (2) A 351 Gr. CF8M (1)

A 182 Gr. F316 (1) A 182 Gr. F316H

A 240 Gr. 316 (1) A 240 Gr. 316H

I 18Cr-13Ni-3Mo 1 A 240 Gr. 317 (1)

lSCr-lONi-3Mo I I A351 Gr.CG8M (3) I NOTES: (1) At temperatures over 1000°F, use only when the carbon content is 0.04% or higher. (2) Not to be used over 850°F. (3) Not to be used over 1000°F.

Class Temp., OF

-20 to loo 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200 1250 1300

1350 1400 1450 1500

206

150

275 235 215 195 170

140 125 110 95 80

65 50 35 20 ... . . . ... . . . . . . . . .

. . .

. . .

. . .

. . .

WORKIF

300

720 620 560 515 480

450 445 430 425 420

420 415 385 350 345

305 235 185 145 115

95 75 60 40

PRESSURES BY CUSSES

400

960 825 745 685 635

600 590 580 570 565

555 555 515 465 460

405 315 245 195 155

130 100 80 55

600

1440 1240 1120 1025 955

900 890 870 855 &45

835 830 775 700 685

610 475 370 295 235

190 150 115 85

sig

900

2160 1860 1680 1540 1435

1355 1330 1305 1280 1265

1255 1245 1160 1050 1030

915 710 555 440 350

290 225 175 125

1500

3600 3095 2795 2570 2390

2255 2220 2170 2135 2110

2090 2075 1930 1750 1720

1525 1185 925 735 585

480 380 290 205

2500

6000 5160 4660 4280 3980

3760 3700 3620 3560 3520

3480 3460 3220 2915 2865

2545 1970 1545 1230 970

800 630 485 345

Fbpvnted from ASME B16.51996 and 1998, by permission of The American Society of Mechanical Engineers. All rights reserved


GENERAL INFO

Nominal Designation

16Cr-12Ni-2Mo

18Cr-8Ni


A 240 Gr. 316L

A 240 Gr. 304L (1)

A 182 Gr. F316L

A 182 Gr. F304L (1)

Class Temp., "F

-20 to 100 200 300 400 500

600 650 700 750 800

850

150

230 195 175 160 145

140 125 110 95 80

65

WORKll

300

600 505 455 415 380

360 350 345 335 330

320

i PRESSURE

400

800 67 5 605 550 51 0

480 470 460 450 440

430

BY CLASSES, psig

600

7 200 1015 910 825 765

720 700 685 670 660

645

900

1800 1520 1360 1240 1145

1080 1050 1030 1010 985

965

1500

3000 2530 2270 2065 1910

1800 1750 1715 1680 1645

1610

2500

5000 4220 3780 3440 3180

3000 2920 2860 2800 2740

2680



N


180-1ONi-Ti A 182 Gr. F321 (2) A 182 Gr. F321H (1)

Castings Plates

A 240 Gr. 321 (2) A 240 Gr. 321H (1)

Class Temp., "F

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 f 200 1250 1300

1350 1400 1450 1500

150

275 245 230 200 170

140 125 170 95 80

65 50 35 20 . . .

...

. . .

. . .

. . .

. . .

. . .

. . .

. . .

. . .

WORKlh

300

720 645 595 550 515

485 480 465 460 450

445 440 385 355 315

270 235 185 140 110

85 65 50 40

PRESSURE!

400

960 860 795 735 685

650 635 620 610 600

595 590 515 475 415

360 315 245 185 145

115 85 70 50

BY CLASSES,

600

1440 1290 1190 1105 1030

97 5 955 930 915 900

895 885 775 715 625

545 475 370 280 220

170 130 105 75

lsig

900

2160 1935 1785 1655 1545

1460 1435 1395 1375 1355

1340 1325 1160 1070 940

815 710 555 420 330

255 195 155 115

1500

3600 3230 2975 2760 2570

2435 2390 2330 2290 2255

2230 2210 1930 1785 1565

1360 1185 925 705 550

430 325 255 190


2500

6000 5380 4960 4600 4285

3980 3880

4060

3820 3760

3720 3680 3220 2970 2605

2265 1970 1545 1170 915

715 545 430 315


GENERAL INFORMATION

Nominal Designation

18Cr-1ONi-Cb



A 182 Gr. F347 (2) A 182 Gr. F347H (1) A 182 Gr. F348 (2) A 182 Gr. F348H (1)

A 351 Gr. CFBC (3) A 240 Gr. 347 (2) A 240 Gr. 347H (1) A 240 Gr. 348 (2) A 240 Gr. 348H (1)

SECTION 9

Class Temp., "F

-20 ro 100 200 300 400 ,500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200 1250 1300

1350 1400 1450 1500

150

275 255 230 200 170

140 125 110 95 80

65 50 35 20 . . .

. . .

. . .

. . .

. . .

. . .

. . .

. . .

. . .

. . .


300

720 660 615 575 540

51 5 505 495 490 485

485 450 385 365 360

325 275 170 125 95

70 55 40 35

400

960 880 820 765 720

685 67 0 660 655 650

645 600 515 485 480

430 365 230 165 7 25

90 75 55 45

~

600

1440 1320 1230 1145 1080

1025 1010 990 985 975

970 900 775 725 720

645 550 345 245 185

135 110 80 70

lsig

900

2160 1980 1845 1720 1620

1540 1510 1485 1475 1460

1455 1350 1160 1090 1080

965 825 515 370 280

205 165 125 105

1500

3600 3300 3070 2870 2700

2570 2520 2470 2460 2435

2425 2245 1930 1820 1800

1610 1370 855 615 465

345 275 205 170

2500

6000 5500 51 20 4780 4500

4280 4200 41 20 4100 4060

4040 3745 3220 3030 3000

2685 2285 1430 1030 770

570 455 345 285

Reprinted from ASME 816.51996 a n d 1998, by permission of The American Society of Mechanical Engineers. All rights reserved


GENERAL I N F O R ~ ~ ~ i


23Cr-12Ni


Plates

A 240 Gr. 309s (1)(2)(3) A 240 Gr. 309H

25Cr-12Ni A 351 Gr. CH8 (1) A 351 Gr. CH20 (1)

NOTES: (1) At temperatures over lOOO"F, use only when the carbon content is 0.04% or higher. (2) Fortemperatures above 1000°F, use only if the material solution is heat treated to the minimum

temperature specified in the specification but not lower than 19OO"F, and quenching in water or rapidly cooling by other means.

(3) This material should be used for service temperatures 1050°F and above only when assurance is provided that grain size is not finer than ASTM 6.

Class Temp., OF

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200 1250 1300

1350 1400 1450 1500

21 0

150

260 230 220 200 170

140 125 110 95 80

65 50 35 20 ...

. . .

. . .

. . .

. . .

. . .

. . .

. . .

. . .

. . .


300

670 605 570 535 505

480 465 455 445 435

425 415 385 335 290

225 170 130 1 00 80

60 45 30 25

400

895 805 760 710 670

635 620 610 595 580

565 555 515 450 390

300 230 175 135 105

80 60 40 30

600

1345 1210 1 I40 1065 1010

955 930 910 895 870

850 830 775 670 585

445 345 260 200 160

115 90 60 50

sig

900

2015 1815 1705 1600 1510

1435 7395 1370 1340 1305

1275 1245 1160 1010 875

670 515 390 300 235

175 135 95 70

1500

3360 3025 2845 2665 2520

2390 2330 2280 2230 2170

2125 2075 1930 1680 1460

1115 860 650 495 395

290 225 155 120


2500

5600 5040 4740 4440 4200

3980 3880 3800 3720 3620

3540 3460 3220 2800 2430

1860 1430 1085 830 660

485 370 260 200


SEC

Nominal Designation

2 5 C r - 2 0 N i


A 351 Gr. CK20 (1) A 182 Gr. F310 (1)(3) A 240 Gr. 310s (1)(2)(3) A 240 Gr. 310H

- ~~ -~ -~ ~~ _ _ _ _ ~ ~ _ _ _ _ ____ ~ ~

NOTES: (1) At temperatures over lOOO"F, use only when the carbon content is 0.04% or higher. (2) For temperatures above lOOO"F, use only i f the material is heat treated by heating it to a

temperature of at least 19OOOF and quenching in water or rapidly cooling by other means. (3) Service temperatures of 105OOF and above should be used only when assurance is provided

that grain size is not finer than ASTM 6.

Class Temp., OF

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 7 200 1250 1300

1350 1400 1450 1500

150

260 235 220 200 170

140 125 110 95 80

65 50 35 20 . . . . . . . . . . . . . . . . . . . . . ... ... . . *


300

670 605 570 535 505

480 470 455 450 435

425 420 385 345 335

260 190 135 105 75

60 45 35 25

400

895 810 760 715 675

640 625 610 600 580

570 555 515 460 450

345 250 185 135 100

80 60 45 35

600

1345 1215 1140 1070 1015

960 935 910 900 87 5

855 835 775 685 67 0

520 375 275 205 150

115 90 65 50

sig

900

2015 1820 1705 1605 1520

1440 1405 1370 1345 1310

1280 1255 1160 1030 1010

780 565 470 310 225

175 135 100 75

1500

3360 3035 2845 2675 2530

2400 2340 2280 2245 2185

2135 2090 1930 1720 1680

1305 945 685 515 375

290 225 165 130

2500

5600 5060 4740 4460 4220

4000 3900 3800 3740 3640

3560 3480 3220 2865 2800

2170 1570 1145 855 630

485 370 275 215



SECTION 9

Castings

9 351 Gr. CK3MCuN

A 351 Gr. CEEMN (1)

A 351 Gr. CD4MCu (1)

A 351 Gr. CD3MWCuN (1)

GENERAL ~ ~ F O R ~ A T ~ O N


Plates

A 240 Gr. S31254

A 240 Gr. S31803 (1)

A 240 Gr. S32750 (1)

A 240 Gr. S32760 (1)

I Forgings Nominal

Designation - ~

2OCr-18Ni-6Mo .

22Cr-5Ni-3Mo-N

25Cr-7 N i -4Mo- N

24Cr-10Ni-4Mo-V

25Cr-5Ni-ZMo-3Cu

25Cr-7Ni-3.5Mo-W-Cb

25Cr-7Ni-3.5Mo-N-Cu-W

A 182 Gr. F44

A 182 Gr. F51 (11

A 182 Gr. F53 (11

A 182 Gr. F55 (1;

150 300

290 750 260 720 230 665 200 61 5 170 57 5

140 555 125 550 110 540 95 530

(1) This steel may become brittle after service at moderately elevated temperatures. Not to be used over 600°F.

400 600 900

1000 1500 2250 960 1440 2160 885 1330 1995 820 1230 1845 770 1150 1730

740 1115 1670 735 1100 1650 725 1085 1625 710 1065 1595

Class Temp., OF

-20 to 100 200 300 400 500

1500

3750 3600 3325 3070 2880

2785 2750 2710 2660

600 650 700 750

2500

6250 6000 5540 5120 4800

4640 4580 4520 4430

21 2

Reprinted from ASME B16.5-1996 and 1998, by permission of The American Society of Mechanical EnGineers. All rinhts reserved



B 462 Gr. NO8020 (1) 35Ni-35Fe-20Cr-Cb

Plates

B 463 Gr. NO8020 (1)

WORKING PRESSURE!

T Qu Tsmp., 'F

-20 10 100 200 300 400 5MI

6W 650 700 750 aw

150

290 260 230 200 170

740 125 110 95 a0

BY CLASSES,

600

750 720 715 675 655

605 590 570 530 510

1500 1440 1425 1345 1310

1210 1175 1135 1065 1015

1000 960 9 50 900 a75

805 785 755 710 675

sig

900

2250 2760 2140 2020 1965

1815 1765 1705 1595 1525

1500

3750 3600 3565 3365 3275

3025 2940

2660 2540

2840


2500

6250 6000 5940 5610 5460

5040 4905 4730 4430 4230



Nominal Designation

99.ONi



€3 160 Gr. NO2200 (1)(2) B 162 Gr. NO2200 (1)

Class Temp., "F 150 300 400 600 900 1500

-20 to 100 140 360 480 720 1080 1800 200 140 360 480 720 1080 1800 300 140 360 480 720 1080 1800 400 140 360 480 720 1080 1800 500 140 360 480 720 1080 1800

600 140 360 480 720 1080 1800

2500

3000 3000 3000 3000 3000

3000



TABLE 2-3.3 RATINGS FOR GROUP 3.3 MATERIALS Nominal

Designation

99.ONi-Low C

Forgings Castings PhteS

B 160 Gr. NO2201 (1)(2) B 162 Gr. NO2201 (1)

Class Temp., O F

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 7 050

1100 1150 1200

150

90 85 85 85 85

85 85 85 80 80

65 50 35 20 . . . . . . . . . . . .


300

240 230 225 215 215

215 215 215 210 205

205 140 115 95 75

60 45 35

400

320 305 300 290 290

290 290 290 280 270

270 185 150 125 7 00

ao 60 50

600

480 455 445 430 430

430 430 430 420 410

410

230 185 150

125 95 75

280

isig

900

720

670 650 650

650 650 650 635 610

610 41 5 345 280 220

185 140 170

685

1500

1200 1140 1115 1080 1080

1080 1 oao 1 oao 1055 1020

1020 695 570 465 370

310 230 185

2500

2000 1900 1860 1800 1800

1800 iaoo 1 aoo 1760 1700

1700 1155 950 770 615

515

310 385

Reprinted from ASME 616.519% and 1998, by permission of The American Society of Mechanical Engineers. All rights reserved


SECTION 9

Nominal Designation

67Ni-30Cu

67Ni-30Cu-S

GENERAL INFORMATION


B 127 Gr. NO4400 (1) 8 564 Gr. NO4400 (1)

B 164 Gr. NO4405 (1)(2)

400

800 705 660 635 635

635 635 635 625 610

455 330

Class Temp., O F 600

1200 1055 990 955 950

950 950 950 935 915

680 495

-20 t o 100 200 300 400 500

600 650 700 7 50 aoo

850 900

150

230 200 190

170

140 125 110 95 80

65 50

1 a5

21 6

300

600 530 495

475

475 47 5 47 5 470 460

340 245

480

WORKING PRESSURES BY CLASSES isig

900

iaoo 1585 1485 1435 1435

1435 1435 1435 1405 1375

1020 740

1500

3000 2640 2470 2390 2375

2375 2375 2375 2340 2290

2500

5000 4400 4120 3980 3960

3960 3960 3960 3900 3820



Nominal Designation

72Ni- 15Cr-8Fe

9


B 564 Gr. NO6600 (1) B 168 Gr. NO6600 (1)

Class Temp., "F

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200

150

290 260 230 200 170

140 125 110 95 80

65 50 35 20 . . .

. . .

. . .

. . .

WORKING PRESSURE!

300

750 7 50 730 705 665

605 590 570 530 510

485 450 325 215 140

95 70 60

400

1000 1000 970 940 885

805 785 755 710 675

650 600 435 290 185

125 90 80

aY CLASSES.

600

1500 1500 1455 1410 1330

1210 1175 1735 1065 1015

975 900 655 430 280

185 135 125

sig

900

2250 2250 2185 2115 1995

1815 1765 1705 1595 1520

1460 1350 980 650 415

280 205 185

1500

3750 3750 3640 3530 3325

3025 2940 2840 2660 2540

2435 2245 1635 1080 695

465 340 310

Reprinted from ASME B16.51996 and 1998, by permission of The American Society of Mechanical Engineers. All riDhts resewed

2500

6250 6250 6070 5880 5540

5040 4905 4730 4430 4230

4060 3745 2725 1800 1155

770 565 515



33Ni-42Fe-210 B 564 Gr. NO8800 (1)

Class Temp., O F

Plates

B 409 Gr. NO8800 (1 )

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200 1250 1300

1350 1400 1450 1500

150

27 5 255 230 200 170

140 125 110 95 80

65 50 35 20 ... ... . . . . . . . . . . . .

. . .

. . .

. . .

. . .


300

720 660 625 600 580

57 5 570 565 530 ,

505

485 450 385 365 360

325 27 5 205 130 60

50 35 30 25

400

960 885 830 800 770

765 760 750 710 675

650 600 515 485 480

430 365 270 175 80

65 45 40 35

600

1440 1325 1250 1200 1155

1145 1140 1130 1065 1015

975 900 775 725 720

645 550 405 260 125

100 70 60 50

;ig

900

2160 1990 1870 1800 1735

1720 1705 1690 1595 1520

1460 1350 1160 1090 1080

965 825 610 390 185

150 100 95 75

1500

3600 3310 3120 3000 2890

2870 2845 2820 2650 2535

2435 2245 1930 1820 1800

1610 1370 1020 650 310

245 170 155 125


2500

6000 5520 5200 5000 4820

4780 4740 4700 4430 4230

4060 3745 3220 3030 3000

2685

1695 1080 515

410 285 255 205

2285



Designation

65Ni-28Mo-2Fe


B 335 Gr. N10665 (1)(2) B 333 Gr. N10665 (1)

Class Temp., OF

-20 to 100 200 300 400 500

600 650 700 750 800

150

290 260 230 200 170

140 125 110 95 80

WORKING PRESSURES BY CLASSES.

300

750 750 730 705 665

605 590 570 530 510

400

1000 1000 970 940 885

805 785 755 710 675

600

1500 1500 1455 1410 1330

1210 1175 1135 1065 1015

sig

900

2250 2250 2185 2115 1995

1815 1765 1705 1595 1520

1500

3750 3750 3640 3530 3325

3025 2940 2840 2660 2540


2500

6250 6250 6070 5880 5540

5040 4905 4730 4430 4230


L


54Ni-16Mo-15Cr B 564 Gr. N10276 (1)(4)

Castings Plates

B 575 Gr. N10276 (1)(4)

60Ni-22Cr-9Mo-3.5Cb

62Ni-28Mo-5Fe

70Ni-16Mo-7Cr-5Fe

61Ni-16Mo-16Cr

42Ni-27.5Fe-3Cr-2.3Cu

B 564 Gr. NO6625 (3")

B 335 Gr. N10001 (1)(2)(6)

B 573 Gr. N10003 (2K3)

B 574 Gr. NO6455 (1)(2)(6)

B 564 Gr. NO8825 (3)(7)

B 434 Gr. N10003 (3)

B 575 Gr. NO6455 (1)(6)

B 424 Gr. NO8825 (3)(7)

B 443 Gr. NO6625 (3")

B 333 Gr. NlOOOl (1)(6)

NOTES: (1) Use solution annealed material only. (2) The chemical composition, mechanical properties, heat treating requirements, and grain

size requirements shall conform to the applicable ASTM specification. The manufacturing procedures, tolerances, tests, certification, and markings shall be in accordance with ASTM B 564.

(3) Use annealed material only. (4) Not to be used over 1250°F. (5) Not to be used over 1200°F. Alloy NO6625 in the annealed condition is subject to severe loss

of impact strength at room temperatures after exposure in the range of 7000°F to 1400°F. (6) Not to be used over 800°F. (7) Not to be used over 1000°F.

Class Temp., 'F

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200 1250 1300

220

150

290 260 230 200 170

140 125 110 95 80

65 50 35 20 ... * . . ... ... . . . ...


300

750 750 730 705 665

605 590 570 530 510

485 450 385 365 360

325 275 185 145 110

400

1000 1000 970 940 885

805 785 755 710 675

650 600 515 485 480

430 365 245 195 145

600

1500 1500 1455 1410 1330

1210 1175 1135 1065 1015

975 900 775 725 720

645 550 370 29 5 215

900

2250 2250 2185 2115 1995

1815 1765 1705 '1595 1520

1460 1350 1160 1090 1080

965 825 555 440 325

1500

3750 3750 3640 3530 3325

3025 2940 2840 2660 2540

2435 2245 1930 1820 1800

1610 1370 925 735 540



2500

6250 6250 6070 5880 5540

5040 4905 4730 4430 4230

4060 3745 3220 3030 3000

2685 2285 1545 1220 900

G


47Ni-22Cr-gMo-18Fe B 572 Gr. NO6002 (1)(2)

Plates

B 435 Gr. NO6002 (1)

s N 9

Class Temp., 7

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200 1250 1300

1350 1400 1450 1500

150

290 260 230 200 170

140 125 110 95 80

65 50 35 20 . . . . . . . . . . . . . . . * . .

. . .

...

. . .

. . .

WORKII

300

750 750 680 600 575

560 560 560 530 510

485 450 385 365 360

325 275 205 180 140

105 75 60 40

PRESSURES

400

1000 1000 905 795 770

745 745 745 710 675

650 600 515 485 480

430 365 275 245 185

140 100 80 55

IY CLASSES,

600

1500 1500 1360 1195 1150

1120 1120 1120 1065 1015

975 900 775 725 720

645 550 410 365 275

205 150 115 85

iig

900

2250 2250 2040 1795 1730

1680 1680 1680 1595 1525

1460 1350 1160 1090 1080

965 825 620 545 410

310 225 175 125

-

1500

3750 3750 3395 2990 2880

2795 2795 2795 2660 2540

2435 2245 1930 1820 1800

1610 1370 1030 910 685

515 380 290 205

2500

6250 6250 5660 4980 4800

4660 4660 4660 4430 4230

4060 3745 3220 3030 3000

2685 2285 1715 1515 1145

860 630 485 345



SE 9

Nominal Designation

25Ni-46Fe-21Cr-5Mo

222


B 672 Gr. NO8700 (1)(2) B 599 Gr. NO8700 (1)

GENE

Class Temp., "F 150 300 400 600 900 1500

-20 to 100 275 720 960 1440 2160 3600 200 260 720 960 1440 2160 3600 300 230 680 905 1360 2040 3400 400 200 640 855 1280 1920 3205 500 170 610 81 5 1225 1835 3060

600 140 595 790 1190 1780 2970 650 125 570 760 1140 1705 2845

2500

6000 6000 5670 5340 5100

4950 4740



GENERAL INFORMATION

Nominal Designation

44Fe-25Ni-21Cr-Mo



B 649 Gr. NO8904 (1)(2) B 625 Gr. NO8904 (1)

Class Temp.. 'F 150 300

-20 to 100 245 640 200 230 600 300 210 545 400 190 495 500 170 455

600 140 430 650 125 420 700 110 410

SECTION 9

400 600 900

855 1280 1920 800 1200 1805 725 1085 1630 660 995 1490 610 91 5 1370

575 865 1295 560 840 1265 545 820 1230

3205 3005 2720 2485 2285

2160 2105 2050

1500 I 2500

5340 5010 4530 4140 3810

3600 3510 3420



SECTION 9

Nominal Designation

26Ni-43Fe-22Cr-5Mo

47Ni-22Cr-20Fe-7Mo

224


B 621 Gr. NO8320 (1)(2)

B 581 Gr. NO6985 (1)(2)

B 620 Gr. NO8320 (1)

B 582 Gr. NO6985 (1)

GENERAL INFORMATION


Class Temp., OF

I

-20 to 100

300 400 500

600 650 125 700 110 750 800


300 I 400 I 600

670 625 585 535 500

475 465 450 445 430 I 1345

1245 1175 1075 1000

950 930 900 885 865

sig

900

201 5 1870 1760 1610 1500

1425 1395 1350 1330 1295

1500

3360 31 15 2935 2680 2500

2375 2320 2250 2215 2160



2500

5600 5190 4890 4470 4170

3960 3870 3750 3690 3600


Designation

49Ni-25Cr-18Fe-6Mo

Ni-Fe-Cr-Mo-Low Cu


B 581 Gr. NO6975 (1)(2)

B 564 Gr. NO8031 (3)

B 582 Gr. NO6975 (1)

B 625 Gr. NO8031 (3)


Class Temp., OF

-20 to 100 200 300 400 500

150 300

290 750 260 705 230 660 200 635 170 595

600 650 700 750 800

600

1500 1410 1325 1265 1190

1125 1105 1085 1065 1015

. -

900

2250 2715 1985 1900 1780

1685 1660 1630 1595 1525

~

400

140 125 110 95 80

1000 940 885 845 790

750 735 725 710 675

560 555 545 530 510

1500

3750 3530 3310 3170 2970

2810 2765 2720 2660 2540

2500

6250 5880 5520 5280 4950

4680 4605 4530 4430 4230



SECTION 9


47Ni-22Cr-19Fe-6 MOB 581 Gr. NO6007 (1)(2)

GENERAL INFORMATION

Castings Plates

B 582 Gr. NO6007 (1)

Class Temp., "F

-20 to 100 200 300 400 500

600 650 700 750 800

850 900 950

1000

226

~ _ _

150

275 245 230 200 170

140 125 110 95 80

65 50 35 20

400

960 860 795 750 715

690 680 675 670 660

650 600 51 5 485


600

1440 1290 1195 1125 1070

1035 1020 1015 1005 995

975 900 775 725

300

720 645 600 560 535

520 510 505 500 495

485 450 385 365

sig

900

2160 1935 1795 1685 1605

1555 1535 1520 1505 1490

1460 1350 1160 1090

1500

3600 3230 2990 2810 2675

2590 2555 2530 2510 2485

2435 2245 1930 1820

2500

6000 5380 4980 4680 4460

4320 4260 4220 4180 4140

4060 3745 3220 3030




Designation

33Ni-42Fe-21Cr


B 409 Gr. NO8810 (1) B 564 Gr. NO8810 (1)

Class Temp., "F

-20 to loo 200 300 400 500

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200 1250 1300

1350 1400 1450 1500

150

230 205 195 185 170

140 125 110 95 80

65 50 35 20 ... * . . . . . ... ... . . . ... . . . . . . ...

WORKII

300

600 540 505 480 455

440 425 420 415 410

400 395 385 365 325

320 275 205 180 140

105 75 60 40

i PRESSURE:

400

800 720 675 640 610

585 565 560 550 545

530 530 515 485 435

430 365 275 245 185

140 100 80 55

BY CLASSES

600

1200 1080 1015 960 910

880 850 840 825 815

795 790 775 725 650

640 550 410 365 275

205 150 115 85

tsig

900

1800 1620 1520 1440 1370

1320 1275 1260 1240 1225

1195 1190 1160 1090 975

965 825 620 545 410

310 225 175 125

1500

3000 2700 2530 2400 2280

2195 2125 2100 2065 2040

1990 1980 1930 1820 1625

1605 1370 1030 910 685

515 380 290 205

Reprinted from ASME B16.5-19% and 1998, by permission of The American Society of Mechanical Engineers. All rights reserved

2500

5000 4500 4220 4000 3800

3660 3540 3500 3440 3400

3320 3300 3220 3030 2710

2675 2285 1715 1515 1145

860 630 485 345



Nominal Designation

35Ni-19Cr-1Y4Si



B 511 Gr. NO8330 (1)(2) B 536 Gr. NO8330 (1)

300 Class

Temp., O F

-20 to 100 200 300 400 500

400

600 650 700 750 800

850 900 950

1000 1050

1100 1150 1200 1250 1300

1350 1400 1450 1500

22%

150

275 245 225 200 170

140 125 110 95 80

65 50 35 20 . . . . . . . . . . . . . . . . * .

. . .

...

. . .

...


720 635 590 550 525

500 490 480 470 465

455 445 385 365 310

240 185 145 115 95

75 55 45 35

960 850 785 735 700

670 655 645 625 620

605 590 515 485 410

320 245 195 155 130

100 75 60 45

600

1440 1270 1175 1105 1050

1005 980 965 940 925

905 885 775 725 615

480 370 290 235 190

150 110 95 70

mig

900

2160 1910 1765 1655 1575

1505 1470 1445 1410 1390

1360 1330 1160 1090 925

720 555 435 350 285

220 165 140 100

1500

3600 3180 2940 2760 2630

2510 2450 2410 2350 2315

2270 2215 1930 1820 1545

1205 925 725 585 480

370 280 230 170



2500

6000 5300 4900 4600 4380

4180 4080 4020 3920 3860

3780 3690 3220 3030 2570

2005 1545 1210 975 795

615 465 385 285

AE

Nominal Designation

29Ni-20.5Cr-3.5Cu-2.5Mo

TABLE 2-3.17 RATINGS FOR GROUP 3.17 MATERIAL


A 351 Gr. CN7M (1)

Cless Temp., 'F 150 300 400 600 900 1500

-20 to 100 230 600 800 1200 1800 3000 200 200 520 690 1035 1555 2590 300 180 465 620 930 1395 2330 400 160 420 565 845 1265 2110 500 150 390 520 780 1165 1945

600 140 360 480 720 1080 1800

2500

5000 4320 3880 3520 3240

3000



SECTION 9

0.1301 0.1486 0.1655 0.1817 0.1924 0.2035 0.2181 0.2299 0.2419

0.1825 02243 0.2223 0.2463 0.2679 0.2884 0.3019 0.3157 0.3339 0.3632

0.2894 0.3167 0.3390 0.3685 0.3948 0.4197 0.4359 0.4525 0.4742 0.5090

GENERAL INFORMATION

0.1636 0.1636 0.1636 0.1636 0.1636 0.1636 0.1636 0.1636 0.1636

0.1963 0.1963 0.1963 0.1963 0.1963 0.1963 0.1- 0.1963 0.1963 0.1963

0.2291 02291 0.2291 0.2291 02291 0.2291 0.2291 O m 1 02291 02291

TABLE D-7

CHARACTERISTICS OF TUBING

1.062 0.969 0.893 0.792 0.703 0.618 0.563 0.507 0.433 0.314

0.607 0.635 0.657 0.685 0.709 0.731 0.745 0.759 0.777 0.805

- hnstant

C** 7

46 52 56 58

94 114 125 134

- B.W.G. Gage

- sq. Ft. Inlcnul SUrfiCC Pa Foot h g h

0.- 0.0539 0.0560 0.0571

7

ansvrme etalArea iq. Inch

O.D. ID. -

1289 1214 1.168 1.147

1.354 1.230 1.176 1.133

~ 0.045

0.040

X C k n t s S Inches

0.0791 0.0810 0.0623 0.0829

22 24 26 27

0.028 0.022 0.018 0.016

0.0296 0.0654

0.0360 0.0654 0.0373 0.0654

0.0333 1 0.0654 0.0195 0.0158 0.0131 0.01 18

0.0502 0.0374 0.0305 0.0244

3.00012 3.00010 I . m 3.cxnYoa 3 . w 3.- D.00046 D.00038

0.0036 0.- 0.025 0.WZO

0.1 166 0.1208 0.1231 0.1250

18 20 22 24

0.171 0277 0.049 0.035 0.028 0.022

0.065 O.M9 0.035 0.028

0.109 0.095 0.083 0.072 0.065 0.058 0.049 0.042 0.035

0.134 0.120 0.109 0.095 0.083 0.072 0.065 0.058 0.049 0.035

168 198 227 241

1.351 1.244 1.163 1.126

0 . W 0.0694 0.051 1 0.0415

0.0969 0.1052 0.1 126 0.1162

0.0021 D.0018 0.W14 0.w12

0.1555 0.1604 0.1649 0.1672

0.0086 0.W71 0.w56 O.ML46

0.0197 0.0183 0.0170 0.0156 0.0145 0.0134 0.0119 0.0105 0.0091

0 . W 0 . m 0.0309 0.0285 0.0262 0.0238 0.0221 0.0203 0.0178 0.0134

0.0505 0.0475 0.0449 0.041 1 0.0374 0.0337 0.0312 0.0285 0.0249 0.01 87

0.0784 0.0700 0.0654 0.0615 0.0559 0.0507 0.0455 0.0419 0.- 0.0247

0.1425 0.1355 0.1187 0.11w 0.1027 0.0926 0.0833 0.0682 0.0534 0.0395 0.1806 0.1545 0.1241 0.1m

- 16 18 x) 22

12 13 14 15 16 17 18 19 20

10 11 12 13 14 15 16 17 18 x)

10 11 12 13 14 15 16 17 18 20

8 10 11 12 13 14 15 16 18 x)

0.141 0.444 0.1548 203 232 258 283 3M) 317 340 359 377

1.536 1.437 1 .m 1299 1263 1228 1.186 1.155 1.126

0.177 0.158 0.141 0.125 0.114 0.103 0.089 0.077 0.065

0.1066 0.1139 0.1202 0.1259 0.1296 0.1333 0.1380 0.1416 0.1453

0.0061 0.0051 0.W53 OLXM.9 0.W45 o.aM2 0.0037 0.W33 O.OO26

0.1665 0.1904 0.1939 0.1972 0.1993 02015 0.2044 OM67 02090

02229 0.2267 02299 02340 0.2376 0241 1 02433 02455 02484 02x31

285 319 347 364 418 450 471 492 521 567

1.556 1.471 1.410 1.339 1 284 1.238 1210 1.183 1.150 1.103

0.259 0.238 0219 0.195 0.174 0.153 0.140 0.126 0.108 0.079

0.1262 0.1335 0.1393 0.1466 0.1529 0.1587 0.1623 0.1660 0.1707 0.1780

0.652 0.680

451 494 529 575 61 6 655 680 706 740 794

1.442 1.378 1.332 1 277 1234 1.197 1.174 1.153 1.126 1.087

0.312 0.285 0.262 0.233 02D7 0.182 0.165 0.149 0.127 0.092

0.134 0.120 0.109 0.095 0.083 0.072 0.065 0.058 0.049 0.035

0.1589 0.1662 0.1m 0.1793 0.1856 0.1914 0.lW 0.1987 0.2036 02107

02362 02703 02736 02778 02815 0.2850 02873 020% 0.2925 02972

0.0221 0.0208 0.0196 0.0180 0.0164 0.0148 0.0137 0.0125 0.0 1 09 0.0082

0.0392 0.0350 0.0327 0.0307 0.0280 0.0253 0.0227 0.0210 0.0166 0.0124

0.0890 0.0847 0.0742 0.0688 0.0642 0.0579 0.0521 0.- 0.0334 0.0247

0.3009 0.3098 0.3140 0.3174 0.3217 0.3255 0.3291 0.3314 0-7 0.3414

550 656 708 749 804 852 698 927 997

1060

1 A93 1.366 1.316 1.279 1235 1.199 1.168 1.149 1.109 1.075

0.433 0.365 0.332 0.305 0270 0239 0.210 0.191 0.146 0.106

0.165 0.134 0.120 0.109 0.095 0.083 0.072 0.065 0.049 0.035

0.5755

0.6793 0.3836 0.3880 0.3974 0.4018 0.4052 0.4097

970 1037 1182 1250 1305 1377 14.40 1537 1626 1706

1.404 1.359 1 273 1.238 1211 1.179 1.153 1.116 1.085 1.059

7 8

10 11 12 13 14 16 18 XI

0.1 80 0.165 0.134 0.120 0.109 0.095 0.083 0.065 0.049 0.035

0.6221 0.3272 0.6648 0.3272 0.7574 0.3272 0.8012 0.3272 0.8365 0.3272 0.8825 0.3272 0.8229 0.3272 0.9852 0.3272 1.0423 0.3272 1.0936 o.sz72

1.1921 0.3927 1.2908 0.3927 1.3977 0.3927 i 1.4741 0.3927

0.605 0.562 0.470 0.426 0.391 0.345 0.304 0242 0.185 0.134

0.575 0.476 0.369 0293

0.709 0.648 0.569 0.500 -

.. .. 0.4136 0.4196 0.4250 0,4297

0.4853 0.4933 0.5018 0.5079

1860 2014 2180 2300

1216 1.170 1.124 1.095

10 12 14 16

0.134 0.109 0.083 0.065

0.1354 0.1159 0.0931 0.0756

0.3144 02604 02586 02300 7

0.3225 03356 0.3492 03581 0.4804 0- 0,44732 o m 1 -

1257 1334 0.997 1.370 .. .

0.3144 02604 02586 02300

0.6660 0.6697 0.6744 0.6784

3795 3891 4014 4121 -

1.136 1.122 1.105 1.091 -

11 12 13 14 -

0.120 0.109 0.095 0.083 -

0.5236

1.701 1 .634

Ay by the following factors: * Weights are based on low carbon steel with a density of 0.2836 1bS.h . in. For 0 t h m d s mu Aluminum Bronze .................................. 1.04 Aluminum Brass ................................... ". 1-06 Nickel-Chrome-Iron ................................. 1-07 Admiralty ................................. ".............. 1.09

Nickel ...................................................... 1.13 Nickel-Copper ........................................ 1.12 Copper and Cupro-Nickels .................... 1.14

Aluminum ................................................ 0.35 Titanium ..................................... . ......_..... 0.58 A.I.S.I. 400 Series SBteels .................... 0.99 A.I.S.I. 300 Series S/Steels .................... 1.02

** Liquid Velocity = lbS. per Tube Hour C x Sp. Gr. of Liquid

in feet per sec. (Sp. Gr. of Water at WF. = 1.0)


Tube O D m m

6 35

9 53

12 7

15 88

19 05

22 23

25 4

31 75

33 1

50 8

B W G Gage

Internal

mm Sq Cm Thickness Area

22 24

18 1245 08187 20 I 0889 I 09368

0711 01910 0559 02148

11723 12413 13129 1 4071

00598 00598 00598 00598 00598 00598 00598

2 il; 1 14832 1 5606

3404 11774 00407 00425 00447 00466 00484 00495 00506

11 12

13 14 15

16 17

05342 05064 04670 04293 03900 03622 03327

3 048 2 789 2 413 2 108 1829 1651 1473

5758 5839 5944 6035 6 124 6180 6236

13181 14342 1 5890 17284 18606 1 9477 2 0368

474 516 572 622 870 701 733

1471 15355 1410 14129 1339 12581 7284 11226 1238 09871 1210 09032 1183 08129

2 0432 2 1871 2 3774 2 5471 2 7077 2 8123 2 9193

775 843

11.54 06968 1103 05097

11 12 13 14 15 16 17

12 2769 53968 13 14 1 ::i 1 :=: 16 6 3561

3 048 2 769 2 413 2 108 1829 1851 1473

TABLE D-7M

CHARACTERISTICS OF TUBING

00698 00698 00698 00698 00698 00698 00698

0 0199

00507 00524 00547 00566 00583 00594 00606

00299 00255 I 00264 00299 00399 00295

07784 07358 06735 06129 05522 05113 04670

0 0499 0 0499

0 0499

6866 6949 7056 7 150 7239 7297 7356

1101 1182 819 977 1053 1115

1126 08194 1087 05935 1493 27935 1366 23548 1316 2 1419 1279 19677

11 12 13 14 15 16

3048 29264 2769 30987 2413 33245 2108 35245 1829 37129 1651 38355

00997 00919 00997 I ",: 0 1197

00798 00798 00798 00798 00798 00798

Weight Per M length Steel

0 098 0 080 0 067 0 060 0 254 0 189 0 155 0 124 0 449 0 351 0 259 0 210 0 894 0 801 0 716 0 634 0 579 0 524 0 449 0 390 0 329 1240 1202 1112 0 990 0 881 0 777 0 708 0 638 0546 0 399 1 580 1 442 1 329 1179 1046 0 920 0 838 0 754 0644 0 467 2 192 1847 1 680 1545 1 368 1211 1063 0 967 0 741 0 537 3064 2 848 2 380 2 158 1 979 1 746 1542 1 226 0 936 0 877 2 912 2 412 1871 1484 3 589 3 280 2 880 2 531

K g *

00607 00624 O W 6 00665 00683 00694

Tube I D m m

4 93 5 23 544 554 704 7 75 8 10 8 41 9 40 10 21 10 92 11 28 10 34 11 05 11 66 12 22 12 57 12 93 13 39 13 74 14 10 12 24 12 95 13 51 14 22 14 83 15 39 15 75 16 10 16 56 17 27 15 42 16 13 16 69 17 40 18 01 18 57 18 92 19 28 19 74 20 45 17 02 18 59 19 30 19 86 20 57 21 18 21 74 22 10 22 91 23 62 22 61 23 37 24 94 25 65 26 21 26 92 27 53 28 45 29 26 29 97 31 29 32 56 33 88 34 80 44 70 45 26 45 97 46 56

18 20 7 8 10 11

Moment of Inertia

cm

0 0050 0 0042 0 0037 0 0033 0 0283 0 0229 0 0191 0 0158 0 0874 0 0749 0 0583 0 0499 0 2539 0 2373 0 2206 0 2040 0 1873 0 1748 0 1540 0 1374 0 1165 0 5369 0 5078 0 4828 0 4454 0 4079 0 3704 0 3455 0 3183 0 2789 0 2081 0 9199 0 8658 0 8158 0 7492 0 6826 0 6160 0 5702 0 5203 0 4537 0 3413 16318 14566 13611 12778 11655 10531 0 9449 0 8741 0 8909 0 5161 3 7045 3 5255 3 0885 2 8637 2 6722 2 4100 2 1686 17732 13902 10281 5 6358 4 8242 3 8751 3 1467 13 0864 12 0874 10 7638 9 5734

*

1245 4 1226 0889 43826 4572 40135 4191 42890 3404 48864 3048 5 1690

0 2999

0 2556

0 2196 0 1950

00997 00997 00997 00997 00997 00997

0 1721 0 1491 0 5637

00784 00806 00824 00846 00865 00694

* 11471

10717 1 0078 0 9160 0 8308 0 7456 0 6866

7 976 8 ffi2 8 171 8 268 8 359 8 418

22205 9855 19452 10094 18026 10206 16830 10292 15175 10406 13651 10505 11176 10658

SE N 9

1 Transverse i Metal

170 185 200

1437 10194 345 1362 09097 384

422 1299 08065 1263 07355 447

472 1228 06645 506 1186 05742 534 1155 04968 562 1126 04194 424 I 1556 I 16710

735

917 974 1012 1050

1196 1235 17419

1268 1336 1 ; ;l I ;= I 1380 1149 12323

1543 1 359 1758

1942 2049 1179

0 6839

3 0323

0 8845 3 7097 3 0710 2 3806

4 1806 5973

* Weights are based on low carbon steel with a density of 7.85 gm/cu.cm. For other metals multiply by the following factors:

Aluminum ....................................... 0.35 Aluminum Bronze ........................... 1.04 Nickel .............................................. I .13 Titanium .......................................... 0.58 Aluminum Brass ............................. 1.06 Nickel-Copper ....__.__....... ~ ..._..........._ 1.12 A.I.S.I. 400 Series %Steels .._...._____. 0.99 Nickel-Chrome-Iron _..........._._.__._._. . 1.07 Copper and Cupro-Nickels ............. 1.14 A.I.S.I. 300 Series S/Steels _...._____... 1.02 Admirality ....................................... 1.09

ka. Per Tube Hour ** Liquid Velocity = c sp. G ~ , ofLiquid in meters per see. (Sp. Gr. of Water at 15.6 deg C = 1.0)


SECTION 9 N

TABLE D-8

HARDNESS C O N V E R S I O N TABLE

APPROXIMATE RELATION BETWEEN VARIOUS HARDNESS TESTING

SYSTEMS AND TENSILE STRENGTH OF CARBON A N D ALLOY STEELS

I -

I Tensile

~ Strenqth lo00 Lbs

PSI

I I I i ROCKWELL HARDNESS NUMBER

1

1 384 j 368

1 309

352 337 1 324

~ 323 318

293 ! 279 , 266 1 259 247 237 226

217 210 202 195 188

182 176 170 166 160

155 1 so 145 141 137

133 129 126 122 118

101 99 97 95 83

91 89 87 I :: ’ 82 80

i 3: I 71

70 1 6 8


S ENERAL INF TI

TABLE D-9

INTERNAL WORKING PRESSURES (PSI) OF TUBES AT VARIOUS VALUES OF ALLOWABLE STRESS -

Tube Gage BWG

Code Allowable Stress (P5

20,000 2,000 4,000 6,000 8,000 10,000 12,000 14.000 16,000 18,000

269 305 378 434 492 570 630 776 929

539 61 1 757 869 984 1140 1261 1552 1859

809 916 1135 1304 1476 1711 1891 2329 2789

1079 1222 1514 1739 1 968 2281 2522 3105 3719

1349 1528 1893 21 73 2460 2852 3153 388 1 4648

1618 1833 2271 2608 2952 3422 3783 4658 5578

1888 2139 2650 3043 3444 3992 4414 5434 6508

2158 2444 3029 3478 3936 4563 5045 621 0 7438

2428 2750 3407 3913 4428 5133 5675 6987 8368

2698 3056 3786 4347 4920 5704 6306 7763 9297

27 26 24 23 22 21 20 19 18

24 22 21 20 19 18 17 16 15 14

22 20 19 18 17 16 15 14 13 12

2462 3176 3663 4034 4920 5836 7060

9073 10758

2345 2966 3602 4253 51 14

6509 7656 8962 10562

2345 2840 3345 4009 4537 5075 5943 6921 8107 9073 10351

am9

5803

- --

1969 2541 2930 3227 3936 4669 5648 6439 7258 8606

1876 2372 2881 3402 4091 4642 5207 6125 7169 8449

1876 2272 2676 3207 3630 4060 4754 5537 6485 7258 8281

221 6 2858 3297 363 1 4428 5253 6354 7244 8166 9682

2110 2669 3241 3828 4603 5223 5858 6891 8066 9505

492 635 732 806 984 1167 1412 1609 1814 2151

469 593 720 850 1022 1160 1301 1531 1792 2112

738 952 1099 1210 1476 1751 21 18 2414 2722 3227

703 889

1 080 1276 1534 1741 1952 2297 2688 3168

1477 1905 2198 2420 2952 3502 4236 4829 5444 6454

1407 1 779 21 61 2552 3068 3482 3905 4594 5377 6337

1407 1704 2007 2405 2722 3045 3566 4153 4864 5444 6210

1723 2223 2564 2824 3444 4085 4942 5634 635 1 7530

1641 2076 2521 2977 3580 4062 4556 5359 6273 7393

1641 1988 2342 2806 31 76 3553 4160 4845 5674 6351 7246

246 317 366 403 492 583 706 804 907 1075

234 296 360 425 51 1 580 650 765 896 1056

984 1270 1465 1613 '

1968 2334 2824 3219 3629 4303

938 1186 1 440 1701 2045 2321 2603 3062 3584 4224

1231 1588 1831 2017 2460 2918 3530 4024 4536 5379

1172 1483 1801 21 26 2557 2901 3254 3828 4481 528 1

1172 1420 1672 2004 2268 2537 2971 3460 4053 4536 51 75

20 19 18 17 16 15 14 13 12 11 10

-

234 284 334 400 453 507 594 692 810 907 1035

469 568 669 801 907 1015 1188 1384 1621 1814 2070

703 852 1003 1202 1361 1522 1783 2076 2432 2722 3105

938 1136 1338 1603 1815 2030 2377 2768 3242 3629 4140

21 10 2556 301 1 3608 4003 4568 5349 6229 7296 8166 9316



TABLE D-S-(ContInued)


Tube Gage BWG

20 18 17 16 15 14 13 12 11 10 9 8

20 18 17 16 15 14 13 12 11 10 9 8

- Tube O.D.

Inches

Code Allowable Stress (PSI)

2,000 4,000 10,Ooo 12,000 16,000 18,OOO 14,000

1357 1930 2308 2607 291 1 3399 3946 4604 5137 5836 6561 7475

1157 1641 1959 221 1 2466 2874 3329 3874 4313 4886 5477 6218

- 3 4

-

775 1102 1318 1489 1663 1942 2255 2631 2935 3335 3749 4271

661 938

1119 1263 1409 1642 1 902 2213 2464 2792 3129 3553

~~

969 1378 1648 1862 2079 2428 2818 3289 3669 4169 4686 5339

826 1172 1399 1579 1761 2052 2377 2767 3080 3490 3912 4441

1745 2481 2967 3352 3743 4370 5074 5920 6605 7504 a435 961 1

1939 2757 3297 3724 4159 4856 5637 6578 7339 8338 9373

10679

1652 2345 2799 3159 3523 4105 4755 5534 6161 6980 7824 8882

1551 2205 2637 2979 3327 3885 4510 5262 5871 6670 7498 8543

1322 1876 2239 2527 2818 3284 3804 4427 4929 5584 6259 7106

387 55 1 659 744 831 971

1127 1315 1467 1667 1874 2135

330 469 559 631 704 821 95 1

1106 1232 1396 1564 1 776

581 827 989

1117 1247 1456 1691 1973 2201 2501 281 1 3203

495 703 839 947

1057 1231 1426 1660 1848 2094 2347 2664

193 275 329 372 41 5 485 563 657 733 833 937

1067

165 234 279 315 352 410 475 553 616 698 782 888

1163 1654 1978 2234 2495 2913 3382 3946 4403 5003 5623 6407

991 1407 1679 1895 21 14 2463 2853 3320 3697 4188 4694 5329

1487 21 10 2519 2843 3171 3695 4280 4980 5545 6282 7042 7994

718

1 20 18 17 16 15 14 13 12 11 10 9 8

-

744 203 243 274 305 355 41 1 477 530 600 671 760

288 407 486 548 61 1 71 1 822 955

1061 1200 1343 1520

432 61 1 729 822 916

1066 1233 1432 1592 1801 2014 2281

576 815 973

1097 1222 1422 1615 1910 21 23 2401 2686 3041

720 1019 1216 1371 1528 1 778 2056 2388 2651 3001 3357 380 1

864 1223 1459 1645 1833 2133 2467 2865 31 85 3602 4029 4562

1008 1427 1703 1919 21 39 2489 2878 3343 3716 4202 4700 5322

1152 1631 1946 2194 2444 2844 3290 3821 4247 4802 5372 6082

1296 1835 2189 2468 2750 3200 3701 4298 4778 5403 6043 6843

1440 2039 2432 2742 3056 3556 4112 4776 5309 6003 671 5 7603


GENERAL INFORMATION

114 161 21 7 24 1 280 323 374 41 5 469 523 590 650

231 308 341 384 428 482

171 227 252 283 314 353

SECTION 9

229 323 434 483 561 647 749 83 1 938 1046 1180 1301

463 617 683 769 856 964

343 455 504 566 629 706

TABLE D-9-(Contlnued)


Tube Gage BWG

20 18 16 15 14 13 12 11 10 9 8 7

14 12 11 10 9 8

14 12 11 10 9 8

-

-

Tube O.D.

Inches

Code Allowable Stress (E'!

16,000 ~

18,000 20,000 6,000

343 485 651 724 841 971 1124 1247 1407 1569 1771 1952

- 8.000 12,000 14.000 10.000

572 809 1085 1207 1402 1618 1874 2079 2345 2615 295 1 3254

1-114 458 647 868 966 1122 1294 1499 1663 1876 2092 2361 2603

687 971 1302 1449 1683 1942 2249 2495 2814 3138 3542 3905

80 1 1133 1519 1690 1963 2265 2624 291 1 3283 3662 4132 4556

916 1295 1736 1932 2244 2589 2999 3327 3752 4185 4722 5207

1031 1456 1953 2173 2524 2913 3374 3743 4221 4708 5313 5858

1145 1618 2170 2415 2805 3236 3749 41 59 4690 5231 5903 6509

1-12 2315 3086 3418 3848 4284 4824

1852 2468 2735 3078 3427 3859

1373 1823 2016 2265 2517 2826

2084 2777 3076 3463 3856 4342

1545 2051 2268 2548 2831 3179

694 925 1025 1154 1285 1447

515 683 756 849 943 1059

926 1 234 1367 1539 1713 1929

686 91 1 1008 1132 1258 1413

1621 2160 2393 2693 2999 3377

1201 1595 1 764 1982 2202 2473

1157 1543 1 709 1924 2142 2412

858 1139 1 260 1415 1573 1 766

1 389 1851 2051 2309 2570 2894

1030 1367 1512 1699 1887 2119

1717 2279 2521 2831 3146 3533

2


EC 9

I MATERIAL 200 C STL. C-MO. MN-MO AUSTENITIC STN STL LOW CHROMES THRU 2% 2-1/4 CR-1 MO & 3 CR-I MO INT CR-MO (5-9% CR)

28.5 27.6 1 29.0 29.8 ' 30.1

28.5 27.1 25.4 17.6 9.6

30.2 27.8 30.3 29.1 29.3

16.6 14.6 15.6 15.0 21.5

30.6 27.3 14.6 13.4 28.8

28.0

-

-

-

-

12. 13, 15 & 17% CR LOW NI STEELS THRU 3-1/2% NI-CU ALLOY 400 (N04400) 90-10 CU-NI (C70600) ALUMINUM

27.4

28.2 27.5 -

NI-CR-FE ALLOY 600 (N06600) NI-FE-CR (NO8800 & NO6810) NI-MO ALLOY (N10001) NI-MO-CR ALLOY C-276 (N10276 NICKEL 200 (N02200)

300 400 500 28.0 27.4 27.0 27.0 26.5 25.8 28.5 27.9 27.5 29.4 28.8 28.3 1

' 29.7 29.0 28.6

27.9 27.3 26.7 26.7 26.1 25.7 25.0 24.7 24.3 17.3 16.9 16.6 9.2 8.7 8.1

29.9 29.5 29.0 27.4 27.1 26.6 29.9 29.5 29.1 28.6 28.3 27.9 28.8 28.5 28.1

16.3 16.0 15.6 14.4 14.1 13.8 15.4 15.0 14.7 14.6 14.0 13.3 21.1 20.7 20.2

30.1 29.8 29.3 26.9 26.6 26.2 14.4 14.1 13.8 12.4 11.5 10.7 28.5 28.1 27.8

____ COPPER & AL-BRONZE COMMERCIAL B W S ADMIRALM TITANIUM 70-30 CU-NI (C71500)

NI-MO ALLOY 8-2 (N10665) NI-FE-CR-MO-CU (N08825) MUNTZ (C36SOO) ZIRCONIUM (R60702) NI-CR-MO-CB (N06625)

7 MO (S32900) 7 MO PLUS [S329sO\

17-19 CR STN STL AL-6XN STN STL (N08367) AL-29-4-2 SEA-CURE 2205 (S3 1 803) 3RE60 (s31500)

TABLE D-10 MODULUS OF ELASTICITY

- 70

29.2 28.3 29.7 30.6 30.9

29.2 27.8 26.0 18.0 10.0

31 .O 28.5 31.1 29.8 30.0 17.0 15.0 16.0 15.5 22.0

31.4 28.0 15.0 14.4 30.0

29.0 29.0

-

-

-

-

-

29.0 28.3 29.0 31.0 29.0 29.0 -

- 1 00 29.0 28.1 29.5 30.4 30.7

29.0 27.6 25.8 17.9 9.9

30.8 28.3 30.9 29.6 29.8

16.9 14.9 15.9 15.4 21.9

31 -2 2 7.8 14.9 13.9 29.3

28.8

-

-

-

-

-

28.1

28.8 28.7 -

PSI x l o t 6

27-5 I I 26.8 26.1 25.5 I I 27.6 26.8 -

27.0 26.0 -

26.6 25.3 -

- 1 600 26.4 25.3 26.9 27.7

1 28.0

26.1 25.2 24.1 16.0

28.7 26.4 28.8 27.6 27.8

15.1 13.4 14.2 12.6 19.6

29.0 25.9 13.4 9.9

27.3

-

-

-

-

-

- - 24.8

26.2 24.5 -

REFERENCES ASME SECTION II, D, 1998 EDITION INTERNATIONAL NICKEL CO. R.A. MOEN (COLLECTED PAPERS, LITERS & DATA) ASTM SPECIAL TECHNICAL PUBLICATION # 181 HUNTINGTON ALLOYS, INC. BULLETIN 15M1-761-42 CARPENTER TECHNOLOGY ALLEGHENY LUDLUM STEEL CORP. TRENT TUBE CABOT-STELLITE AIRCO, INC. TELEDYNE WAH CHANG ALBANY SANDVIK TUBE


NERAL INF TI0

426.7 482.2 164.8 153.1 166.2 162.0 175.8 171.0 181.3 176.5 180.0 170.3

170.3 160.0 158.6 147.5 159.3 155.8

190.3 186.2 175.1 171.0 191.0 186.8 182.7 178.6 184.1 180.0

77.2

192.4 188.2 171.7 168.2

180.0 175.8

TABLE D-10 M MODULUS OF ELASTICITY

537.8 593.3 648.9 138.6 122.7 105.5 157.2 152.4 t46.2 164.8 158.6 150.3 169.6 163.4 155.1 156.5 140.7 125.5

148.2 131.7 114.5 135.8 120.7 105.5 152.4 149.6 146.2

182.0 178.6 174.4 166.9 164.1 160.0 182.0 179.3 174.4 174.4 171.7 167.5 175.8 173.1 168.9

184.1 180.6 176.5 164.1

173.1 168.9 165.5

21.1 137.8 93.3 196.5 190.3 199.9 205.5 207.5

196.5 186.8 175.1 121.3 66.2

148.9 204.4 193.1 188.9 186.2 182.7 196.5 192.4 202.7 198.6 204.8 199.9

192.4 188.2 184.1 18O.C 172.4 170.2 119.3 116.5 63.4 60.C

315.6 182.0 174.4 185.5

193.1

180.0 173.7 166.2 110.3

191.0

197.9 182.0 198.6 190.3 191.7

104.1 92.4 97.9

135.1

199.9

92.4 68.3

188.2

86.9

178.6

171.0

180.6 168.9

371.' 174.4 171.0 181.3

188.2

176.5 169.6 163.4 106.2

186.8

194.4 178.6 195.1 186.e 188.2

100.C 88.2 94.5

129.E

197.2

88.2

184.1

82.0

175.8

166.2

164.1

I f

C STL, C-MO, MN-MO AUSTENITIC STN STL LOW CHROMES THRU 2%

IN1 CR-MO (5-9% CR)

12. 13. 15 & 17% CR

NI-CU ALLOY 400 (N04400) 90- 10 CU-Nt (C70600) ALUMINUM

2-1/4 CR-1 MO & 3 CR-1 MO

LOW NI STEELS THRU 3-1/2%

TP 439 STN STL AL-GXN STN STL (N08367) AL-29-4-2 SEA-CURE 2205 (S31803) 3RE60 (S31500)

201.3 199.: 195.1 193.7 204.8 203.4

213.0 211.1

201.3 199.9

179.3 177.9 124.1 123.4 68.9 68.3

211.0 209.6

191.7 190.3

199.9 195.1 199.9 213.7 199.9 199.9

NI-CR-FE AtLOY 600 (N06600) NI-FE-CR (NO8800 & N08810) NI-MO ALLOY B (Nl0001) NI-MO-CR ALLOY C-276 (N10276) NICKEL 200 (N02200)

COPPER dr AL-BRONZE COMMERCIAL BRASS ADMIRALTY TITANIUM 70-30 CU-NI (C71500)

193.7

198.5 197.9

213.7 212.4 196.5 195.1 214.4 213.C 205.5 204.1 206.8 205.5

117.2 116.5 103.4 102.7 110.3 109.6 106.9 106.2 151.7 151.0

I I

208.2 191.7 208.9 200.6 202.0

114.5 100.7 107.6 103.4 148.2

211.0 188.2 100.7 92.4

198.6

193.1

188.9

194.4 189.6

REFERENCES: ASME SECTION II. D. 1998 EDITION

206.2 203.4 788.9 186.€ 206.2 203.4 197.2 195.1 198.6 196.5

112.4 110.3 99.3 97.2

106.2 103.4 100.7 96.5 145.5 142.7

207.5 205.5 185.5 183.4 99.3 97.2 05.5 79.:

196.5 193.7

189.6

184.8 180.0

190.3 186.1 184.8 179.2

kPa X 10''

NI-MO ALLOY 6-2 (N10665) NI-FE-CR-MO-CU (N08825) MUNTZ ((36500)

NI-CR-MO-CB (N06625)

7 MO (S32900) 7 MO PLUS fS32950)

ZIRCONIUM (R60702)

216.5 215.1 193.1 191.7 103.4 102.7

206.8 202.C

199.9 198.6 199.9

99.3 95.8

- 260.t 186.2 177.9 189.6 195.1 197.2

184.1 177.2 167.5 114.5 55.8

-

-

199.9 183.4 200.6 192.4 193.7

107.6 95.1

101.4 91.7

139.3

202.0 180.6 95.1 73.8

191.7

-

-

-

175.8

183.4 174.4 -

INTERNATIONAL NICKEL CO. R.A MOEN (COLLECTED PAPERS.-LETTERS & DATA) ASTM SPECIAL TECHNICAL PUBLICATION # 181 HUNTINGTON ALLOYS, INC. BULLETIN # 15M1-76T-42 CARPENTER TECHNOLOGY " ALLEGHENY LUDLUM STEEL CORP. CABOT - STELLlTE TELEDYNE WAH CHANG ALBANY

TRENT TUBE AIRCO, INC. SANDVIK TUBE


SECTION 9

1200

8.24

7.97 7.64 7.08 6.88 6.44 6.65

10.40 10.29 9.85 1056 9.47 9.40

8.80

12.10

7.44 8.08

GENERAL INFORMATION

1300

6.74

10.52 10.39 9.90

10.66 9.54 9.51

8.90

7.63 a12

9.60 maxi

TABLE D-11 MEAN COEFFICIENTS OF THERMAL EXPANSION

Ih

C-SI 3L. C-1/2 UO h 1 CR-1/2 YO 5.60 5-64

UN-UO Sn 5.60 6.08 C-UN-SI 31 1 1/4-1/2 Yo &3 CR-1 W

2-1/2 h 3-1/2 NI

2-1/4 CR-1 M 5.60 5.90 5 CR-1/2 uo 5.60 5.90 7 CR-1/2 UO & 9 CR-1 hi0 5.60 5.68 12 CR h 13 CR 5.10 5.39 15CRh 17CR 5.10 5.19 17-19 CR (TP 439)

UL GRADES OF TP 316 dr 317 STN STl UL GRAllf3 OF TP 304 STN STL ULCRNlEfOFTP321STNSn UL CRADES of TP 347 STN Sn 25 CR-12 NI, 23 CR-12 NI h 25 CR-20 NI U-6XN (NO8367) UUUINUU (MOJ) 11.80 12.04 ALwmuY (6061) 11.80 12.06 TiTANlUU (OES 1.2.3 It 7) NI-CU (NWHX)) NI-CR-FE (NO6WO)

NI-FE-CR (NO6800 &. N08810) NI-FE-CR-M-CU (N08825) NI-UO (UlW 8) NI-YO-CR (ULM C-276) “10276) NICKEL (UlM 200) (NO2200) 22G5 (S31803)

6.20 6.39

3RE60 (S31500) 70-30 CU-NI (C71500) 90-10 & 80-20 CU-NI COPPER Blws UUUINUU BRONZE

7 UO RUS (y29sO)

CORJER-SKICON mwTY zIR(XwIUU CR-M-FE-UO-CU-CB (ULm 2KB) NI-CR-UO-CB (KLW 625) (NO6625) U 29-4-2 SA-CURE

7 (u2900)

CHFS PER INCH PER OEG F X lO-’BElWfEN 70 F AND.

8.50 8.n:

5.60 6.m

INTERNATIONAL NICKEL CO.

1100 - a0 7

- 7.90 756 7.00 6.83 6.37 6.56

10.29 10.18 9.79

10.45 9.41 9.29

7

-

-

8.70

7

11.90

7.25 7.98 -

8.00

IEFERENCES: ASME SECTION I t , D, 1998 EDITION R A MOEN (COLLECTED PAPERS, LETTERS dt DATA) ASTM SPECIAL TECHNICAL PUBLICATION 181 HUNTINGTON ALLOYS, INC. BULLETIN # 1 SM 1 -76T-42 CARPENTER TECHNOLOGY ALLEGHENY LUDLUM STEEL CORP. TRENT TUBE CABOT-STELLITE AlRCO, INC. TELEDYNE WAH CHANG ALBANY SANDVlK TUBE BRIDGEPORT BRASS COMPANY NATIONAL BUREAU OF STANDARDS SABIN CROCKER, PIPING HANDBOOK, 4TH EDITION D.G. FURMAN, JOURNAL OF METALS


140t 7

-

6.83

10.62 10.49 9.95

10.75 9.62 9.60

-

7

-

8.90

-

7.81 8.16 -

&fo

-

GENERAL INFORMATION

TABLE D-11 M MEAN COEFFICIENTS OF THERMAL EXPANSION

SECTION 9

REFERENCES: ASME SECTION 11, D, 1998 EDITION R.A. MOEN (COLLECTED PAPERS, LEllERS & DATA) HUNTINGTON ALLOYS, INC. BULLETIN #15M1-76T-42 ALLEGHENY LUDLUM STEEL CORP. CABOT-STELLITE TELEDYNE WAH CHANG ALBANY BRIDGEPORT BRASS COMPANY W I N CROCKER, PIPING HANDBOOK, 4TH EDITION

INTERNATIONAL NICKEL CO. ASTM SPECIAL TECHNICAL PUBLICATION # 181 CARPENTER TECHNOLOGY TRENT TUBE AIRCO. INC. SANDVlK TUBE NATIONAL BUREAU OF STANDARDS D.G. FURMAN. JOURNAL OF METALS


AL INFORMATI

700

24.6 23.0 20.8 20.7 19.0

17.2 16.0 22.3 15.9 14.8

13.4

11.8 11.0 11.4 10.6 11.5 11.0

31.8 18.9 11.6 10.1 9.6

8 9 9.2

11.2

47.0 27.0

8.6

13.7

TABLE 0-12 THERMAL CONDUCTIVITY OF METALS

800 900 lo00

23.5 22.5 21.4 22.2 21.4 20.4 20.2 19.7 19.1 20.2 19.7 19.1 18.7 18.4 18.0

17.3 17.2 17.1 16.1 16.1 16.1 21.6 20.9 20.1 15.9 15.9 15.8 14.8 14.8 14.8

13.5 13.6 13.7

122 12.7 13.2 11.5 12.0 12.4 11.9 12.3 12.8 11.1 11.6 12.1 12.0 11.3

32.5 33.1 33.8 19.8 20.9 22.0 12.1 12.6 13.2 10.6 11.1 11.6 10.0 10.4 10.9

8.7 9.3 10.0 9.8 10.4 11.0

11.2 11.3 11.4

49.0 51.0 53.0 30.0 33.0 37.0

9.1 9.6 10.1

UATERlM

CARBON STEEL C-1/2 UOLY STEEL 1 CR-1/2 UO h 1-1/4 CR-1/2 UO 2-1/4 CR-1 UO 5 CR-1/2 UO

- -. 7 CR-1/2 UO 14.1 9 CR-1 UO 12.8 3-1/2 NICKEL 22.9 12 CR & 13 CR 15.2 15 CR 14.2

17 CR 12.6 17-19 CR (TI' 439) TP 304 STN STL 8.6 TP 316 & 317 STN STL 7.7 TP 321 & 347 STN SL 8.1 Tp 310 STN STL 7-3 2205 (S31803) a 0 3x60 (Ul500) 8.4

NICKEL 200 NI-CU (N04400) 12.6 NI-CR-FE (NO6600) 8.6 NI-FE-CR (No8800) 6.7 NI-FE-CR-YO-CU (Nogs25)

NI-YO ALLOY 8 NI-YO-CR NLOY C-276 (N10276) ALUYINUU ALLOY jooJ 102.3 ALUUINUU ALLOY 6061 96.1 MANIUU (GRADES 1.2.3 & 7) 12.7

ADYIRALTY NAVAL BIWS COPPER 90-10 CU-NI 70-30 CU-NI (C71SOO) 7 UO (Uzsoo) 7 uo PLUS (s329so)

NUNTZ ZlRcOMlUV CR-UO ALLOY XU-27 CR-NI-FE-NO-CU-CB (ALLOY ZOCB) NI-CR-NO-CE (ALLOY 625) 5.7 AL 29-4-2 8.8 SEA-CURE 9.4 AL-6XN (N08367)

14.4 15.3 16.0 16.5 13.1 14.0 14.7 15.2 23.2 23.8 24.1 23.9 15.3 15.5 15.6 15.8 14.2 14.4 14.5 14.6

12.7 12.8 13.0 13.1

8.7 9.3 9.8 10.4 7.9 8.4 9.0 9.5 8.4 8.8 9.4 9.9 7.5 8.0 8.6 9.1

8.5 9.0 9.4 9.8

38.8 37.2 35.4 12.9 13.9 15.0 16.1 8.7 9.1 9.6 10.1 6.8 7.4 8.0 8.6

7.1 7.6 8.1

6.1 6.4 6.7 7.0 5.9 6.4 7.0 75

102.8 104.2 105.2 106.1 96.9 99.0 100.6 101.9 125 12.0 11.7 119

70.0 75.0 79.0 71.0 74.0 77.0

225.0 225.0 224.0 30.0 31.0 34.0 18.0 19.0 21.0

8.8 9.3 9.8 10.3 8.6 9.4 10.2 11.1

14.0

8.5 9.0 9.5 10.0

71.0 12.0 11.3 7.6

5.8 6.2 6.8 7.2

9.6 10.3 10.9 11.6 7.9

REFERENCES: ASME SECTION II. 0. 1998 EDITION HUNTINGTON ALLOY, INC. BULLETIN # 15M1-76T-42 A.I.M.E. TECH. PUBLICATIONS NOS 291, 360 & 648 ALLEGHENY LUDLUM STEEL CORP. TELEDYNE WAH CHANG ALW TRANS. AS.S.T. VOL. 21, PAGES 1061-1078 BABCOX fk WlLCOX co.

6.6 5.8 8.2 5.3 4.8

3.9

4.0 3.3 3.7 3.1

4.3 2.7 1.8

12.1

11.0

- 500 26.6 24.3 21.7 21.4 19.2

16.9 15.6 23.4 15.8 14.7

-

- 16.2 15.6 16.9 15.1 14.8

14.1

14.5 13.8 14.1 13.6

143 13.2 12.4

11.5

13.2

10.9 10.0 10.4 9.6

10.5 10.2

34.1 17.0 10.6 9.1 8.6

-

7.4 a1

11.3

84.0 80.0

224.0 37.0 23.0 1 0.8

-

?!

- 600 25.6 23.7 21.3 21.1 19.2

-

17.1 15.9 22.9 15.9 14.7

13.3

11.3 10.5 10.9 10.1 11.0 10.6

32.5 17.9 11.1 9.6 9.1

-

7.7 8.7

11.2

89.0 83.0 '23.0 42.0 25.0 11.3 12.7

-

-

8.2

12.9

4R. FT. OEC. F.

AMERICAN BRASS CO. TRENT TUBE AIRCO, INC. MOT-STELLITE CARPENTER TECHNOLOB INTERNATIONAL NICKEL CO. SANDVIK TUBE

1100 20.2 19.5 18.5 18.5 17.6

-

16.8 16.0 19.2 15.6 14.8

13.8

13.6 12.9 13.3 12.6

-

- 13.8 12.1 11.4

10.7 11.5

-

11.6

-

10.6

200

9.0 8.4 7.7 8.0 7.1

- 1300

17.6 16.7 16.5 17.2 16.6

- - 400 16.2 l5.3 5.0 5.6

I 6.0

5.6 15.2 1 5.5 15.0 4.8

14.3

14.9 14.2 14.6 14.1

-

-

-

15.5 13.8 12.9 -

-

12.0

- 500 5.6 5.0 4.8 5.3 5.8

5.5 5.0 5.3 5.1 4.8

4.5

5.3 4.6 5.0 4.5

-

-

- 6.0 4.5 3.6 -

-

2.6


TABLE D- 12 M THERMAL CONDUCTIVITY OF METALS

TWP. DEG C 1 W/M DEG. c

1 @,-1/2 UO & 1-1/4 CR-1/2 YO 36.9 372 2-1/4 CR-I UO 362 36.3 5 cR-1/2 uo 292 299

7 cR-1/2 UD 24.4 243 9 a-1 w 222 22.7 3-1/2 NtcKEL 39.6 402 12 CR & 13 W 263 265 ' 15 CR 24.6 24.6 17 CR 218 22.0 17-19 CR 439) TP3MsrNn 14.9 15.1 TP 316 h 317 STN !in 133 13.7 TP 321 k 347 STN STL 14.0 145 Tp 310 SIN RL 12.6 13.0 22M (s31803) 138 14.7 3REw (Ulsoo) 145 14.7

N m 2m NI-CR-FE (m) 14.9 15.1 nr-ar (NO1400) 218 223

u-FE-CR (EKlgBoo) w-FE-CR-yo-CU (!@!&?5)

M-MI KLM B 10.6 M-YD-CR lvLM C-276 (Nt0276) 702 KuyasWKLM3w3 177.1 177.9 luuvgJWAuM6061 1663 167.7 MWUY W E S 12.3 h 7l 22.0 21.6

AWSRKM I WVM 3 R G COWER 90-10 (XI-HI 70-30 (XI-M fC71500)

7 uo Rus (u2eso) 149

VUNn ifiRamw CR-Lu) Kurl XU-27

7 hfo tsszsoat 152

CR-NI-R-UO-al-CB (Wm 2ocB) N+cR-uo-cB (am ms) 9.9 10.0 u. 29-4-2 15.2 su-CURE 163 16.6 Al-m (fuJ8367)

REFERENCES ASME SECTION 11, D, 1998 EDITION

S 3 3

2 2 4 2 2 2 2 1 1 1 1 1 1

f

-

-

- 1

1 1

7.9 38.1 37.9 37.6 36.9 36.0 35.0 34-1 33.1 32.0 30.6 6.9 37.2 372 37.0 36.5 35.8 35.0 34.1 33.1 32.0 312 13 32.4 33.1 33.2 332 32.9 32.4 31.3 31.2 305 29.6 6.5 27.7 28.6 292 29.6 298 299 298 29.6 29.1 28.7 4.2 25.4 26.3 27.0 275 27.7 273 27.9 27.9 27.7 27.3 1.2 41.7 41.4 405 39.6 3&6 37.4 562 348 332 315 68 27.0 27.3 273 275 275 275 27.5 27.3 27-0 26.5 4.9 25.1 25.3 25.4 25.4 25.6 256 25.6 25.6 25.6 25.6 2.2 225 22.7 228 2.XO 232 23.4 235 23.7 23-9 24.1 I42

45 15.6 16.4 17.3 18.2 19.0 199 20.6 215 22.3 23.0

38 14.9 157 16.6 175 18-4 192 20.1 20.9 218 22.7 5 6 16.4 173 182 19.0 399 20.8 15.6 16.3 17.0 17.7 18.3 '19.0 19.6

i7.2 64.4 61.3 59.0 56.2 55.0 562 57.3 ~ 585 14.1 26.0 27.9 29.4 31.0 32.7 345 36.2 381 15.7 16.6 175 1$.4 t92 20.1 209 21.8 228 23.9 24.7 2.8 13.8 14.9 15.7 16.6 175 18.4 192 20.1 209 22-0 2 3 13.2 14.0 14.9 15.7 16.6 17.3 1 8 0 183 19.7 20.4 1.1 11.6 12.1 128 13.3 142 15.1 16.1 173 18.5

La3 182.1 183.6 r13 174.1 176.4 !OB 202 19.9 19.6 19.4 19.4 19.4 19.6 19.7 20.1

!1.l 1298 336.7 t45.4 lssn 2.9 128.1 133.3 138.5 143.6 B.4 389.4 s7.7 587.7 38!L9 il.9j U 7 588 64.0 72.7 813 IUS 883 91.7 $12 32.9 36.3 398 433 46.7 519 57.1 64.0 16.1 1711 178 18.7 19.6 I63 17.7 192 29.4 220

a29 20.8 19.6 13.2 10.7 11.8 I 2 5 13.3 14.2 149 15.7 16.6 17.5 18.3 19.C

17.8 18.9 20.1 21.3 223 23.7 13.7

6.1 17.0 180 rag 19.6 20.4 21.1 22.0 228 2s 242

u 16.3 t7.1 iao ias 19.7 20.6 2 1 2 n;! 2u) 23.7

t I

1.1 12.1 1311 14.0 1%; 159 17.0 iao 19.0 199 mg

1 , I

19.0

WERiCAN BRASS CO. 76T-42 TRENT TUBE ~UNTiNGTON ALLOY, INC. B U U m N 115M1

A1.M.E. TECH. PtfBLICAliONS NOS 291. 360 & 648 ALLEGHENY LUDLUM STEEL CORP. W T - S T E L U T E TELEDYNE WAH CHANG ALBANY TRANS, ASS-T. VOL. 21, PAGES 1061-1078 W C O X & WlLCOX co.

AIRCO, INC.

CARPENTER TECHNOLOGY I N T E R ~ n ~ ~ NICKEL CO. W D W K TUBE

-

w)3 280 27.0 28.9 265 26.0 28.6 26.0 zfx6 298 27.0 265 28.7 27.7 273

280 27.0 268 27.0 263 26.0 292 26.8 26.5 26.1 26.0 26.1 25.6 25.6 25.6 24.4 24.7 25.1

25.r 258 265 23.9 24.6 25.3 24.4 25.3 26.0 23.5 24.4 25.1

I

258 268 27.7 22.8 23-9 25.1 215 223 23.5

29.9 M8 21.8


TABLE P13

Weight per Diunetu Inch of

WUGKlS OF CIRCULAR RINGS AND DISCS') Example: Required: Weight of a Ring 48' OD x 36 1 /2' ID x 2 1 /r Thick W diameter disc 1' thick weighs

Ring Wx 36 l /Y x l'weighs Ring Wx36 1/2*x 2 1/2'weighs

513.19 Ibs 296.74 Ibs 21 6.45 Ib 541.13 I b

36 1/2' diameter disc 1' thick weighs

Diameter

Incha I Pounds 1 Inchu

0.000 0.125 0.250 0.375 0.500 0.625 0.750 0.875

0.00 0.00 0.01 0.03 0.06 0.09 0.13 0.17

0.22 0.28 0.35 0.42 0.50 0.59 0.68 0.78

1 .Ooo 1.125 1.250 1.375 1.500 1.625 1.750 1 .875

4.000 4.125 4.250 4.375 4.500 4.625 4.750 4.875

5.000 5.125 5.250 5.375 5.500 5.625 5.750 5.875

13.000 13.125 13.250 13.375 13.500 13.625 13.750 13.875

14.000 14.125 14.250 14.375 14.500 14.625 14.750 14.875

15.000 15.125 15.250 15.375 15.500 15.625 15.750 15.875

37.64 38.37 39.10 39.85 40.59 41.35 4211 4288

43.66 44.44 45.23 46.03 46.83 47.64 48.46 49.28

50.12 50.96 51.80 52.65 53.51 54.38 55.25 56.13

Weight per Inch of

ThidmUl Pound#

2.000 2125 2250 2.375 2.500 2625 2750 2.875

3.000 3.125 3.250 3.375 3.500 3.625 3.750 3.875

3.56 3.79 4.02 4.26 4.51 4.76 5.03 5.29

0.89 6.000 1.01 6.125 1.13 6.250 1.26 6.375 1.39 6.500 1.53 6.625 1.68 6.750 1 .a4 6.875

2.00 7.000 2.18 7.1 25 2.35 7.250 2.54 7.375 2.73 7.500 2.93 7.625 3.13 7.750 3.34 7.875

5.57 5.85 6.14 6.44 6.74 7.05 7.36 7.69

8.02 8.36 8.70 9.05 9.41 9.78

10.15 10.53

10.01 11.31 11.71 121 1 12.53 12.95 13.38 13.81

Diamuer

InChU

8.000 8.125 8.250 8.375 8.500 8.625 8.750 8.875

9.000 9.125 9.250 9.375 9.500 9.625 9.750 9.875

10.000 10.125 10.250 10.375 10.500 10.625 10.750 10.875

11.000 11.125 11.250 1 1.375 11.500 1 1.625 11.750 11.875

Weight per lnch of

ThidmCIS Pounds

14.26 14.70 15.16 15.62 16.09 16.57 17.05 17.54

18.04 18.55 19.06 19.58 20.10 20.63 21.17 21.72

2227 22.83 23.40 23.98 24.56 25.15 25.74 26.34

26.95 27.57 28.19 28.82 29.46 30.10 30.75 31.41

12.000 12125 12.250 12375 12500 12.625 12750 12.875

3207 3275 33.42 34.1 1 34.80 35.50 36.21 36.92

(1) Weights are based on low carbon steel with a density of 0.2836 Ibpnch '. For other metals, multiply by the following factors:

Aluminum ............................................................. 0.35 liunium ................................................................ 0.58 A.I.S.I. 400 Series S/S~ecis .................................. 0.99 A.I.S.I. 300 Series SlSreclr .................................. 1.02 Aluminum Bronze ................................................ 1.W Naval Rolled Brass ................................................ 1.07

Munu: Metal ................................................... "... 1.07 Nickel-Chrome-Iron ................_..-...._.............. .. .... 1.07 Admiralty - ........_..............................-. - ..... -.-..-.- 1-09 Nickel ...-..................................-........-........ ".-"." 1.13 Nickel-Copper ....................I_.I...._..........-~.........-. .. 1.12 Copper & a p r o Nickels ................................... - 1.14


GENERAL INFORMATION SECTION 9

TABLE D-lj--.(Conllnued)

WEIGHTS OF CIRCULAR RINGS AND DISCS

Weight per

Thickness Pounds

Diameter Weight per

Diameter Inch of

Pounds

Weight p r Inch of

Thickness Pounds

Weight per Inch of

Thickness Pounds

98.23 99.40

100.58 101.77 102.96 104.16 105.37 106.58

Diameter

Inches

Diameter

Inches

21.000 21.125 21.250 21.375 21.500 21.625 21.750 21.875

31 .000 31.125 31.250 31.375 31.500 31.625 31.750 31.875

214.05 215.78 2 1 7.52 219.26 221.01 222.77 224.53 226.31

16.000 16.125 16.250 16.375 16.500 16.625 16.750 16.875

57.02 57.92 58.82 59.73 60.64 61.56 62.49 63.43

26.000 26.125 26.250 26.375 26.500 26.625 26.750 26.875

150.57 152.02 153.48 154.95 156.42 157.90 159.38 160.88

162.38 163.88 165.40 166.92 168.45 169.98 171.52 173.07

22.000 22.1 25 22.250 22.375 22.500 22.625 22.750 22.875

107.81 109.03 1 10.27 11 1.51 1 12.76 1 14.02 1 15.28 116.55

32.000 32.125 32.250 32.375 32.500 32.625 32.750 32.875

228.08 229.87 231.66 233.46 235.27 237.08 238.90 240.73

17.000 17.125 17.250 17.375 17.500 17.625 17.750 17.875

64.37 65.32 66.28 67.24 68.21 69.19 70.18 71.17

27.000 27.1 25 27.250 27.375 27.500 27.625 27.750 27.875

117.83 119.11 120.40 121.70 123.01 124.32 125.64 126.96

33.ooo 33.125 33.250 33.37s 33.500 33.625 33.750 33.875

34.000 34.125 34.250 34.375 34.500 34.625 34.750 34.875

242.56 244.40 246.25 248.11 249.97 251.84 253.71 255.60

257.49 259.38 261.29 263.20 265.12 267.04 268.97 270.91

18.000 72.1 7 18.125 73.17 18.250 74.19 18.375 75.21 18.500 76.23 18.625 77.27 18.750 78.31 18.875 79.35

19.ooo 80.41 19.125 81.47 19.250 82.54 19.375 83.61 19.500 84.70 19.625 85.79 19.750 86.88 19.875 87.99

2o.ooo 89.10 20.125 90.21 20.250 91.34 20.375 92.47 20.500 93.61 20.625 94.75 20.750 95.90 20.875 97.06

23.000 23.125 23.250 23.375 23.500 23.625 23.750 23.875

24.000 24.125 24.250 24.375 24.500 24.625 24.750 24.875

25.000 25.1 25 25.250 25.375 25.500 25.625 25.750 25.875

28.000 174.63 28.125 176.19 28.250 177.76 28.375 179.34 28.500 180.92 28.625 182.51 28.750 184.1 1 28.875 185.71

29.Ooo 187.32 29.125 188.94 29.250 190.57 29.375 192.20 29.500 193.84 29.625 195.48 29.750 197.14 29.875 198.80

30.Ooo 200.47 30.125 202.14 30.250 203.82 30.375 205.51 30.500 207.20 30.625 208.90 30.750 210.61 30.875 21 2.33

128.30 129.64 130.98 132.34 133.70 135.07 136.44 137.82

139.21 140.61 142.01 143.42 144.84 146.26 147.69 149.13

35.Ooo 35.125 35.250 35.375 35.500 35.625 35.750 35.875

272.86 274.81 276.77 278.73 280.71 28269 284.67 286.67


Pounds

288.67 290.68 292.69 294.71 296.74 298.78 300.82 302.87

304.93 306.99 309.06 311.14 313.23 315.32 31 7.42 319.52

321.64 323.75 325.88 328.01 330.15 332.30 334.46 336.62

I Inches

41.000 41.125 41.250 41.375 41.500 41.625 41.750 41.875

42.000 42.125 42.250 42.375 42.500 42.625 42.750 42.875

43.000 43.1 25 43.250 43.375 43.500 43.625 43.750 43.875

GIENERAL I io

TABLE D-1 WConilnuod)


Diameter Weigbr per

mdrnes1 Inchof /I Diameter Diameter Diameter

Weight per

mcknesr +& of

Weight per

Thtdme11 Pounds

+ch of

hchw Pounds

374.42 376.71 379.00 381.30 383.61 385.93 388.25 390.58

~-

51 .000 51.125 51.250 51.375 51.500 51.625 51.750 51.875

36.Ooo 36.125 36.250 36.375 36.500 36.625 36.750 36.875

46.000 46.125 46.250 46.375 46.500 46.625 46.750 46.875

471.32 473.88 476.6 479.03 481.62 484.21 486.81 489.42

579.34 582.19 585.04 587.90 590.76 593.63 596.51 599.39

602.29 605.19 608.09 61 1.00 613.92 616.85 619.79 622.73

37.000 37.1 25 37.250 37.375 37.500 37.625 37.750 37.875

392.91 395.25 397.60 399.96 402.32 404.69 407.07 409.45

47.000 47.1 25 47.250 47.375 47.500 47.625 47.750 47.875

52.000 52.125 52.250 52.375 52.500 52.625 52.750 52.875

492.03 494.65 497.28 499.91 502.55 505.20 507.86 51 0.52

513.19 51 5.87 518.55 521.24 523.94 526.64 529.35 532.07

38.000 38.1 25 38.250 38.375 38.500 38.625 38.750 38.875

411.84 414.24 416.65 419.06 421.48 423.90 426.34 428.78

53.000 53.125 53.250 53.375 53.500 53.625 53.750 53.875

625.67 628.63 631.59 634.56 637.53 640.52 643.51 646.50

48.000 48.125 48.250 48.375 48.500 48.625 48.750 48.875

49.000 49.125 49.250 49.375 49.500 49.625 49.750 49.875

39.000 39.125 39.250 39.375 39.500 39.625 39.750 39.875

338.79 340.96 343.14 345.33 347.53 349.73 351.94 354.16

- ~

44.000 44.125 44.250 44.375 44.500 44.625 44.750 44.875

45.000 45.125 45.250 45.375 45.500 45.625 45.750 45.875

431.22 433.68 436.14 438.60 441.08 443.56 446.05 448.54

54.Ooo 54.125 54.250 54.375 54.500 54.625 54.750 54.875

649.51 652.52 655.53 658.56 661.59 664.63 667.67 670.73

673.79 676.85 679.92 683.00 686.09 689.19 692.29 695.39

-.

534.80 537.53 540.27 543.01 545.77 548.53 551 .29 554.07

556.85 559.64 562.43 565.23 568.04 570.86 573.68 576.51

40.000 40.1 25 40.250 40.375 40.500 40.625 40.750 40.875

356.38 358.61 360.85 363.10 365.35 367.61 369.87 372.14

451.05 453.56 456.07 458.60 461.13 463.66 466.21 468.76

50.000 50.125 50.250 50.375 50.500 50.625 50.750 50.875

55.000 55.125 55.250 55.375 55.500 55.625 55.750 55.875


912.34 915.91 919.48 923.06 926.65 930.24 933.85 937.46

94 1.07 944.69 948.32 951.96 955.61 959.26 962.91 966.58

69.000 1060.46 69.125 1064.31 69.250 1068.16 69.375 1072.02 69.500 1075.88 69.625 1079.76 69.750 1083.k 69.875 1087.53

70.m 1091.42 70.125 1095.32 70.250 1099.23

1103.15 70.375 70.500 1107.07 70.625 1111.00 70.750 11 14.93 70.875 11 18.88

TABLE D-l3-(Contlnuod)


I Diameter

Weight per Weight per

Thickness Thickness Inchof I/ Diameter 1 Inchof Diameter

Weight per Inch of

Thickness

Weight per Inch of

Thickness Pounds

1122.83 1 126.78 1 130.75 1 134.72 1 138.70 1142.68 1 146.67 1 150.67

Dimcter

Inches

56.000 56.125 56.250 56.375 56.500 56.625 56.750 56.875

Pounds lnchCJ Pounds 11 Inches 1 Pounds Inches

61 .000 61.125 61.250 6 1 375 61.500 6 1.625 61.750 61.875

828.81 832.21 835.62 839.03 842.45 845.88 849.32 852.76

71 .ooO 71.125 71.250 71.375 71.500 71.625 71.750 71.875

698.51 701.63 704.76 707.90 71 1.04 714.19 71 7.34 720.51

970.25 973.93 977.62 981.31 985.01 988.71 992.43 996.15

66.000 66.125 66.250 66.375 66.m 66.625 66.750 66.875

I

723.68 726.86 730.04 733.23 736.43 739.64 742.85 746.07

62000 62.125 62250 62375 62500 62.625 62.750 62.875

856.21 859.66 863.13 866.60 870.07 873.56 877.05 880.55

~ -

67.000 67.1 25 67.250 67.375 67.500 67.625 67.750 67.875

~

999.88 1003.61 1007.35 1011.10 1014.85 101 8.62 1022.39 1026.16

72.000 72.1 25 72.250 72.375 72.50 72.625 72.750 72.875

1154.68 1158.69 1162.71 1166.74 1 170.77 1174.81 1178.86 118291

57.000 57.1 25 57.250 57.375 57.500 57.625 57.750 57.875

58.m 58.125 58.250 58.375 58.500 58.625 58.750 58.875

59.000 59.125 59.250 59.375 59.500 59.625 59.750 59.875

60.Ooo 60.125 60.250 60.375 60.500 60.625 60.750 60.875

749.29 752.53 755.77 759.01 762.27 765.53 768.80 772.07

63.00 63.125 63.250 63.375 63.500 63.625 63.750 63.875

884.05 887.56 891.08 894.61 898.14 901.68 905.22 908.78

68.m 68.125 68.250 68.375 68.500 68.625 68.750 68.875

1029.84 1033.73 1037.53 1041.34 1045.15 1048.96 1052.79 1056.62

73.000 73.125 73.250 73.375 73.500 73.625 73.750 73.875

1 186.98 1191.04 1195.12 1199.20 1203.29 1207.39 121 1.49 1215.60

775.35 778.64 781.94 785.24 788.55 791.87 795.19 798.52

64.000 64.125 64.250 64.375 64.500 64.625 64.750 64.875

1219.72 1223.84 1227.97 1232.11 1236.26 1240.41 1244.57 1248.73

74.000 74.1 25 74.250 74.375 74.500 74.625 74.750 74.875

75.000 75.1 25 75.250 75.375 75.500 75.625 75.750 75.875

601.86 805.20 808.56 81 1.91 815.28 810.65 822.03 825.42

65.Ooo 65.125 65.250 65.375 65.500 65.625 65.750 65.875

1252.91 1257.09 1261.27 1265.47 1269.67 1273.88 1278.09 1282.31


Diameter

hChU

Weight per Inch of

Pounds ?hicknCS8

76.000 76.1 25 76.250 76.375 76.500 76.625 76.750 76.875

77.000 77.125 77.250 77.375 77.500 77.625 77.750 77.875

Diunuu-

Inchu

78.000 78.1 25 78.250 78.375 78.500 78.625 78.750 78.875

79.000 79.125 79.250 79.375 79.500 79.625 79.750 79.875

80.Ooo 80.125 80.250 80.375 80.500 80.625 80.750 80.875

1286.54 1290.78 1295.02 1299.27 1303.52 1307.79 1312.06 1316.33

1320.62 1324.91 1329.21 1333.51 1337.83 1342.14 1346.47 1350.80

1355.14 1359.49 1363.84 1368.21 1372.57 1376.95 1381.33 1385.72

TABLE D-33+Contlnuocl)

WOGHTS OF CIRCULAR RINGS AND DISCS

81 .000 81.125 81.250 81 375 81.500 81.625 81.750 81.875

82.000 82.125 82.250 82.375 82.500 82.625 82750 82.875

83.000 83.125 83.250 83.375 83.500 83.625 83.750 83.875

1647.38 165217 1656.97 1661.78 1666.59 1671.41 1676.24 1681.07

1685.91 1690.76 1695.61 1700.48 1705.34 171 0.22 1715.10 1719.99

1724.89 1729.79 1734.70 1739.62 1761.55 1749.48 1754.42 1759.36

1764.32 1769.27 1774.24 1 m.21 1784.19 1 789.1 8 1794.18 1799.18

1804.19 1809.20 1814.22 181 9.25 1824.29 1829.33 1834.38 1839.44

91 .000 1844.50 91.125 1849.57 91.250 1854.m 9 1 375 1859.73 91.500 1864.83 91.625 1869.92 91.750 1875.03 91.875 1880.14

92.000 1885.26 92125 1890.39 92250 1895.52 92375 1900.66 92500 1905.81 92625 1910.96 92750 1916.13 92875 1921.29

93.000 1926.47 93.125 1931.65 93.250 1936.84 93.375 1942.04 93.500 1947.24 93.625 195245 93.750 1957.67 93.875 196289

94.Ooo 1968.12 94.125 1973.36 84.250 1978.60 94.375 1983.86 94.500 1999.11 94.625 1994.38 94.750 1999.65 94.875 2006.93

Q5.OOO 2010.22 95.125 2015.51 95.250 2020.81 95.375 2026.12 95.500 2031.43 95.625 M36.76 95.750 2042.08 95.875 2047.42

1390.11 1394.52 1398.93 1403.34 1407.77 1412.20 1416.63 1421.08

84.000 84.125 84.250 84.375 84.500 84.625 84.750 84.875

1425.53 1429.99 1434.45 1438.92 1443.40 1447.89 1452.38 1456.88

85.m 85.125 85.250 85.375 85.500 85.625 85.750 85.875

Weight pe Inch of

Thidmu8 Pormdl

1461.39 1465.90 1470.42 1474.95 1479.49 1484.03 1488.58 1493.13

1497.70 150227 1506.88 1511.43 151 6.02 1520.61 1525.22 1529.83

1534.45 1539.07 1 W.71 1548.35 155299 1 m7.64 156230 1566.97

1571.65 1576.33 1581.01 1585.71 1590.41 1585.12 1599.84 1604.56

1609.29 1614.03 1618.77 1623.52 1628.28 1633.04 1637.81 1642.59

hchU

86.Ooo 86.125 86.250 86.375 86.500 86.625 86.750 86.875

87.000 87.125 87.250 87.375 87.500 87.625 87.7tjO 87.875

88.Ooo 88.125 88.250 88.375 88.500 88.625 88.750 88.875

89.000 89.125 89.250 89.375 89.500 89.625 89.750 89.875

90.000 90.125 90.250 90.375 90.500 90.625 90.750 90.875


SECTION 9

Weight per Diameter h c h of

TABLE P13--(Contlnuod)

WUGHTS OF CIRCULAR RINGS AND DISCS

DiUW2tJX

Inches Pounds lnchu

96.000 96.125 96.250 96.375 96.500 96.625 96.750 96.875

99.Ooo 99.125 99.250 99.375 99.500 99.625 99.750 99.875

100.000 100.125 100.250 100.375 100.500 100.625 100.750 100.875

2052.76 2058.1 1 2063.47 2068.83 2074.20 2079.58 w.96 2090.35

2183.06 104.000 2188.58 104.125 2194.10 104.250 2199.63 104.375 2205.17 104.500 2210.72 104.625 2216.27 104.750 2221.82 104.875

2227.39 105.OOO 2232.96 105.125 2238.34 105.250 2244.13 105.375 2249.72 105.500 2255.32 105.625 2260.93 105.750 2266.54 105.875

101.000 101.125 101.250 101.375 101.500 101.625 101.750 101.875

2646.36 2652.43 2658.51 2664.60 2670.70 2676.80 2682.90 2689.02

2695.14 2701.27 2707.41 271326 2719.70 2725.85 2732.02 2738.19

97.000 97.125 97.250 97.375 97.500 97.625 97.750 97.875

88.000 98.125 98.250 98.375 98.500 98.625 98.750 98.875

114.000 114.125 1 14.250 114.375 1 14.500 114.625 114.750 114.875

115.000 115.125 1 15.250 1 15.375 115.500 1 15.625 115.750 1 15.875

2095.75 2101.16 2106.57 21 11.99 2117.41 2122.84 2128.28 2133.73

21 39.18 2144.65 2150.11 2 155.59 2161.07 2166.56 21 72.05 2177.56

102.000 102125 102.250 102.375 102.500 102.625 102750 102875

103.OOO 103.125 103.250 103.375 103.500 103.625 103.750 103.875

Weight per Inch of

Thicknus Pouuds

2272.16 2277.79 2203.42 2289.06 2294.71 2300.37 m.03 231 1.70

2317.38 2323.06 2328.75 2334.45 2340.15 2345.06 2351.58 2357.31

2363.04 2368.78 2374.52 2380.28 n66.04 2391.80 2397.58 2403.36

2409.14 2414.94 2420.74 2426.55 2432.36 2438.19 2444.02 2449.85

2455.70 2461.55 2467.40 2473.27 2479.14 2485.02 2490.90 2496.80

Diameter

InChU

106.000 106.125 106.250 106.375 106.500 106.625 106.750 106.875

107.000 107.125 107.250 107.375 107.500 107.625 107.750 107.875

108.000 108.125 108.250 108.375 108.500 108.625 108.750 108.875

109.000 109.125 109.250 109.375 109.500 109.625 109.750 109.875

11o.oOo 110.125 110.250 110.375 1 10.500 110.625 110.750 110.875

Weight per

Thiclaress Pounds

Diameter

2502.69 2508.60 2514.51 2520.43 2526.36 253229 2538.24 2564.18

111.000 111.125 11 1.250 1 1 1.375 11 1.500 1 11.625 11 1.750 111.875

2550.14 2556.10 256207 2568.04 2574.03 2580.02 2586.01 259202

2598.03 2604.04 2610.07 2616.10 2622.14 2628.18 2634.24 2640.30

112000 112125 1 12.250 1 12375 112500 1 12625 112750 1 12.875

1 13.000 113.125 113.250 113.375 113.500 113.625 1 13.750 1 13.875


Weight per Inch of

Thicknus Pounds

2744.37 2750.55 2756.74 2762.94 2769.15 2775.36 2781.58 2787.80

2794.04 2800.28 2806.52 281278 2819.04 2825.31 2031.58 2037.06

2844.15 2850.45 2856.75 2863.06 2869.38 2875.70 2882.03 2888.37

2894.72 2901.07 2907.43 2913.79 2920.16 2926.54 2932.93 2939.32

2965.72 2952.13 2958.54 2964.96 2971.39 2977.83 2984.27 2990.72

247

SECTION 9

- C -

1.34278 .34378 .34477 .34577 ,34676

.34776 ,34876 .34975 .35075 ,35175

.35274

.35374

.35474

.35373

.35673

.35773

.U873

.35972

.36072

.36172

.36272

.36372

.36471

.36571

.3667 1

.36V 1

.36871

.36971

.37071 .37171

.372?0

.37370

.37470 .37570 .37670

.37770

.37870

.37970

.38070

.38170

.38270

.38370 ,38470 .38570 .38670

.38770

.38870

.38970

.39070

.391?0 ,39270 --

GENERAL INFOR

-__. C

1.00004 .00012 .00022 .00034

.00047

.00062 ,00078 .00095 .00113

,00133 .00153 ,00175 ,00197 .00220

,00244 ,00268 .00294 .00320 ,00347

.00375

.OM03

.00432 ,00462 .00492

00523 .00555 .00587 ,00619 .00653

.00687

.00721

.00756

.00791

.00827

,00864 .00901 .00938 .00976 .01015

.01054

.01093 ,01133 .01173 .01214

.01255 -01297 .01339 .01382 01425

h/D 0.050

.051 .052 .053 ,054

.055 ,056 ,057 ,058 ,059

.060 ,061 .062 .063 .064

,065 .066 .067 ,068 .069

.070

.071 .072 .073 ,074

.075

.076

.077

.078

.079

,080 .081 ,082 .083 .084

.085

.086

.087

.088

.089

,090 .091 .092 ,093 .094

.095

.096

.097

.W8

.099

C

1.24498 24593 24689 .21784 .24880

.24976 ,25071 25167 .25263 . a359

25455 25551 25647 . a 7 4 3 .2S839

3 9 3 6 .26032 26128 .26225 26321

26418 26514 .26611 ,26708 26805

.26901

.26998 27095 ,27192 ,27289

.27386 ,27483 .27580 ,27678 ,27775

.27872 ,27969 ,28067 ,28164 .28262

.28359

.28457

.28554 ,28652 ,28750

.28848 ,28945 .29043 ,29141 .29239

TABLE D-14 CHORD LENGTHS &AREAS OF ClRCUtAR SEGMENTS

h/D 0.400

.401

.402

.403

.404

,405 .406 .407 .408 .409

.410

.411 ,412 .413 ,414

.415

.416

.417

.418

.419

.420

.421

.422

.423

.424

,425 .426 427 ,428 .429

.430

.431 ,432 .433 .434

,435 ,436 ,437 .438 ,439

,440 .441 ,442 ,443 ,444

,445 ,446 .447 ,448 -449

r h/D

0.00 1 ,002 .003 ,004

,005 .OD6 ,007 .008 ,009

.010

.01 I

. o n ,013 .Ol4

.015 ,016 ,017 .ole .019

.020 ,021 .022 .023 .024

.025

.026 ,027 .028 .029

.030

.031

.032 ,033 ,034

,035 .036 ,037 .038 .039

,040 ,041 .042 ,043 .044

,045 ,046 -047 ,048 ,049

-

-

C

1.04087 .04148 ,04208 .04269 .04330

,04391 .044S2 .04514 .04576 .04638

.04701 ,04763 .04826 ,04889 .04953

,05016 .05080 ,05145 ,05209 .OX74

.05338 .05404 .05469 .05535 .05600

.05666

.OS733 ,05799 .OM66 .05933

.06000

.OW67 .06135 ,06203 ,06271

,06333 ,06407 ,06476 .06545 .06614

.06683

.06753

.06822 ,06892 .06963

.Of033

.07103 ,07174 .07245 .07316

h/D 0.150 .151 .152 .153 .154

.155 ,156 .I57 .158 ,159

.160 ,162 .162 .I63 .164

.165

.166 .167 .168 .169

.170

.171

.172

.173

.174

.175

.176

.177

.I78 .179

.I80

.181

.I82 .183 .184

.185

.186

.187

.I88 ,189

,190 .191 .192 ,193 .194

.195

.196 .197 .198 -199

I

.ZOO92 ,20184

.20276

.20368

.20460

.20553 ,20645

,20738 .20830 .20923 .21015 .21108

.21201 ,21299 .21387 21480 .21573

.21667 ,21760 .21853 21947 .22040

.22134

.22228

.22322

.22415

.22509

.22603 22697 ,22792 .22886 ,22980

,23074 .23169 .23263 .23358 .23453

.23547

.23642

.23737

.23832

.23927

,24022 ,24117 .24212 .24307 ,24403

A = AREA D = DIAMETER h = HEIGHT k = CHORD

.353

.354

.355

.356

.357

.358 ,359

,360 .361 .362 .363 ,364

.365 ,366 .367 .368 .369

.370 ,371 .372 .373 ,374

,375 ,376 .377 ,378 .379

.380

.381

.382

.383 ,384

.385 ,386 .387 .388 .389

.390 ,391 ,392 .393 .394

.395 ,396 .397 ,398 ,399

,01691 .01737 .01783 ,01830 ,01877

- C

.073P7

.07459 ,07531 ,07603 .07675

.07747 ,07819 ,07892 .07965 .08038

,08111 .08185 ,08258 .08332 ,08406

,08480 ,08554 .08629 .OW04 ,08779

.O8854

.08923

.09004

.0908C

.0915!

.09231

.09307 ,09384 .0946( .09531

.0961:

.0969C ,09761 ,0984: ,0992;

.I oooc

.1007i

.1015! ,1023: .1031;

1039C .I0461 ,10547 .1062f .1070!

,10784 .lo864 1094: 1102:

,1110:

-

.lo5

.I06 ,107 ,108 .lo9

- 1/D

,200 .201 ,202 203 ,204

,205 206 .207 ,208 ,209

,210 2 1 1 ,212 .213 214

2 1 5 216 ,217 218 219

,220 221 ,222 223 ,224

,225 226 2 2 7 228 ,229

230 ,231 232 ,233 ,234

,235 .236 ,237 .238 ,239

240 .241 .242 ,243 ,244

245 .246 ,247 248 .249

-

.01924 ,01972 .02020 .02068 ,02117

,02166 .02215 .02265 .02315 .02366

C

1.11182 .11262 ,11343 ,11423 .11504

.11584

.I1665 ,11746 ,11827 .11908

.11990 ,1207 1 .12153 .12235 ,12317

12399 ,12481 ,12563 ,12646 ,12729

,12811 ,12894 .I2977 .I3060 .13144

,13227 .13311 ,13395 ,13478 ,13562

.13646

.13731

.13815

,13984

.14069

.I4154

.14239 ,14324 14409

14494 14580 14666

.14751 14837

,14923 .15009 .I5095 .15182 ,15268

-

. m o o

,110 ,111 .I12 . l l 3 ,114

.llS

.116

.I17 ,118 .119

h / D 0.250 251 ,252 .253 254

2 5 5 .256 257 2 5 8 ,259

,260 .261 262 263 ,264

265 266 ,267 .268 .269

2 7 0 271 2 7 2 2 7 3 ,274

.275 276 .277 ,778 279

280 ,281 ,282 ,283 ,284

,285 286 .287 ,288 ,289

290 .291 ,292 293 ,294

295 .296 ,297 .298 ,299

-

.02417 ,02468 .02520 ,02571 .02624

.02676 ,02729 .02782 ,02836 ,02889

.Om43

.02998

.03053

.Of108 ,03163

,03219 ,03275 .03331 ,03387 ,03444

,03501 ,03555 .03616 ,03674 .03732

.03791’

.03850 ,03909 ,03968 .04028

C

,15355 ,1544 1 .15528 ,15615 .15702

,15789 .15876 ,15964 ,1605 1 ,16139

.I6226 ,16314 .16402 ,16490 .I6578

.16666

. I6735

.16843 ,16932 .17020

.I7109 ,17198 ,17287 .I7376 .17465

.17554

.17644

.17733 ,17823 ,17912

t1800i .la092 .18182 .18271 18361

,18452 .la541 ,18633 . la723 ,18814

,18905 -18996 .1908E ,19177 ,19268

,19360 ,19431 ,19542 ,19634 .19725

-

.I20

.121 .122 .123 .124

,125 .126 .127 .128 .129

:I30 .I31 ,132 .133 .134

,135 .136 ,137 ,138 ,139

.140 ,141 ,142 .143 . I 4 4

,145 .146 .147 ,148 .149

- V D

.300

.301 ,302 .303 .304

,305 ,306 ,307 .308 .309

.310

.31 I

.312 ,313 ,314

.315 ,316 .317 ,318 ,319

,320 ,321 .322 .323 ,324

.325

.326 ,327 .328 .329

.330

.331

.332

.333 ,334

,335 ,336 .337 .338 ,339

,340 ,341 ,342 ,343 ,344

,345 .346 ,347 ,348 .349

-

-

A = C X D ~

k = 2[h( D - h ) y 2

- C

3.29337 ,29435 29533 29631 .29729

.29827 29926 ,30024 ,30122 .30220

,30319 ,30417 .30516 ,30614 .30712

.30811

.309iO

.31008

.31107 ,31205

.3 1304

.31403 ,31502 ,31600 .3 1699

-

,31798 .31837 ,31996 .32095 32194

f32293 ,32392 .3249 1 .32590 .32689

.32788

.32887

.32987

.33086

.33185

33284 .33384 ,33483 ,33582 .33682

.33781 ,33880 33980 34079 ,34179

- V D - ,450 ,451 .452 .453 ,454

.455 ,456 ,457 ,458 ,459

.460

.461 ,462 ,463 .4M

.465 ,466 ,467 .468 .469

,470 .471 ,472 .473 ,474

.475

.476

.477

.478 ,479

A80 ,481 ,482 ,483 ,484

.485 ,486 ,487 .188 ,489

,490 ,491 .492 .493 ,494

,495 ,496 ,497 ,498 ,499 ,500


GENERAL INFORMATION

TABLE D-15

CONVERSION FACTORS

LENGTH

BY 2.540 25.40 30.48 0.3048 0.9144 1.6094

- TO OBTAIN Centimeters Millimeters Centimeters Meters Meters Kilometers

MULTIPLY Inches Inches Feet Feet Yards Miles

- AREA

- BY 6.4516

TO OBTAIN Square Centimeters Square Centimeters Square Meters Square Meters

MULTIPLY Sauare Inches Square Feet Square Feet Square Inches

929.034 0.0929034 0.00064516

VOLUME

- B Y 16.3871 62 0.02831 6 28.316 3.7853 4.54509 0.1589873 0.003785

TO OBTAIN Cubic Centimeters Cubic Meters Liters Liters Liters Cubic Meters Cubic Meters

MULTIPLY Cubic Inches Cubic Feet Cubic Feet Gallons (U. S. Llq.) Gallons (Imp.) Barrels (U. S.) Gallons (U. S. Llq.)

BY

453.592 28.3495

TO OBTAIN Grams Grams Kilograms

MULTIPLY Ounces (AV.) Pounds (AV.) Pounds (AV.) 0.453592

DENSITY

- B Y 27.680 16.01846 16.01794 0.119826

MULTIPLY Pounds Per Cubic Inch Pounds Per Cubic Foot Pounds Per Cubic Foot Pounds Per Gallon (U. S. Liq.)

TO OBTAIN Grams Per Cubic Centimeter Kilograms Per Cubic Meter Grams Per Liter Kilograms Per Liter

VELOCITY

- BY 0.30480 0.00508

MULTIPLY Feet Per Second Feet Per Minute

TO OBTAIN Meters Per Second Meters Per Second

FORCE

- BY

0.004448

MULTIPLY

Pounds-Force

TO OBTAIN

Kilonewtons

VISCOSITY

- BY 0.4133

MULTIPLY Pounds Per Foot-Hour Pounds Per Foot-Hour Pounds Pet Foot-Second Square Feet Per Second Pound-Second Per Square Foot

TO OBTAIN Centipoises Kilogram-Second Per Square Meter Centipoises Centistokes Centipoises

0.0004133 1488.16 92903.04 47900

TEMPERATURE

TO OBTAIN Degrees Fahrenheit

Degrees Rankine Degrees Fahrenheit

Subtract 32 and Divide by 1.8 Divide by 1.8 Add 459.67 and Divide by 1.8

Degrees Centigrade Degrees Kelvin Degrees Kelvin



TABLE D-lS-(Continued)

CONVERSION FACTORS

PRESSURE

TO OBTAIN Kilograms Per Square Centimeter

MULTIPLY Pounds Per Square Inch

- BY 0.070307 4.8828 Kilograms Per Square Meter

Newtons Per Square Meter Bars Pascals Kilograms Per Square Centimeter Kilopascals

Pounds Per Square Foot Pounds Per Square Inch Pounds Per Square Inch Pounds Per Square Inch Inches of Hg Pounds Per Square Inch

6894.76 0.06894 6894.76 0.03453 6.8947

FLOW RATE

BY 0.00006309 - TO OBTAIN

Cubic Meters Per Second Kilograms Per Second Cubic Meters Per Hour Kilograms Per Second

MULTIPLY Gallons Per Minute (U. S. Liq.) Pounds Per Hour Cubic Feet Per Minute Pounds Per Minute

0.0001260 1.69901 1 0.007559

SPECIFIC VOLUME

TO OBTAIN Cubic Meters Per Kilogram L%ers Per Kilogram

MULTIPLY Cubic Feet Per Pound

BY 0.062428 -

Gallons Per Pound (US. Llq.) 8.3454

ENERGY a POWER

MULTIPLY BTU BTU BTU Foot Pound BTU Per Hour

- BY 1055.06 0.2520 0.000252 1.3558 0.29307

TO OBTAIN Joules Kilocalories Thermies Joules watts

ENTROPY

MULTIPLY BTU Per Pound-OF

__. BY 4.1868

TO OBTAIN Joules Per Gram-" C

ENTHALPY

TO OBTAIN Joules Per Gram

MULTIPLY BTU Per Pound

- BY 2.326

SPECIFIC HEAT

MULTIPLY BTU Per Pound-OF

BY r(.1868

TO OBTAIN Joules Per Gram-' C

HEAT TRANSFER

MULTIPLY BTU Per HourSouare Foot-OF

- BY 5.67826

TO OBTAIN Watts Per Square Meter-* C

BTU Per Square Foot-tiour BTU Per Square Foot-Hour BTU Per Square Foot-Hour-°F

3.15459 2.71246 4.88243

Watts Per Square Meter Kilocalories Per Square Meterdour Kilocalories Per Square Meterdour-" C

THERMAL CONDUCTIVITY

MULTIPLY BTU Per FootHour. OF

BY 1.7307 0.14422 1.488

- TO OBTAIN Watts Per Meter-" C

BTU Per Square Foot-*F Per Inch BTU Per Square FootHour O F Per Foot

Watts Per Meter-" C Kilocalories Per Square Meterdour a C Per Meter

FOULING RESISTANCE

MULTIPLY Hour-Square Foot-OF Per BTU Hour-Square F0at-V Per BTU

- BY 176.1 102

TO OBTAIN Square Meter-* C Per Kilowatt Square Meter- Hour ' C Per Kilocalorie 0 .2w

MASS VELOCITY

MULTIPLY Pounds Per Hour-Square Foot

BY 0.0013562

TO OBTAIN Kilograms Per Square Meter-Second

HEATING VALUE

MULTIPLY BTU Per Cubic Foot

BY 0.037259 - TO OBTAIN

Megajoules Per Cubic Meter


GENERAL INFORMATI

us. strrl wm A m k ~ (A.W.G.) (S.W.G.) or Birmingham

B m m urd Shupc or Rocbling or ( f a S r c t l W i n k S W I d d Bimunghun Wm Gage (B. & S.) Am Stat (SS.W.G.) Stubs Iron Wire (fur rhcu d

m4 hoop mud) sundud) (for non-furnus md Wire Co. (for ixon or WUT urd Bcu) I [A. (Sd) W.G.] brur wire)+ wrought uon)

or Wuhbum and M w r (B.W.G.) US. StM&Id hpcrid SUndml

(Britkh legd (B.G.)

(for rhea Md

(far rml m)

0.4900 0.500 0.6666 0.500 0.4815 0.469 0.8250 0.484 0.4305 0.438 0.5883 0.432

0.460 0.3938 0.454 0.406 0.5416 0.400 0.410 0.3625 0.425 0.375 0.5000 0.372 0.365 0.3310 0.380 0.344 0.4452 0.348 0.325 0.3085 0.340 0.312 0.3964 0.324

0289 0.2830 0.300 0281 0.3532 0.300 0.258 0.2625 0284 0286 0.3147 0.276 0229 02437 0259 0250 02804 0252

0238 0234 02500 0.232 0212

0.204 02253 0.182 02070 0.220 0.219 02225

0.182 0.1920 O M 3 0.203 0.1981 0.192 0.144 0.1770 0.180 0.188 0.1764 0.176 0.128 0.1620 0.165 0.172 0.1570 0.180 0.1 14 0.1483 0.148 0.156 0.1398 0.144 0.102 0.1350 0.134 0.141 0.1250 0.128

0.091 0.1205 0.120 0.125 0.1 113 0.1 16 0.081 0.1055 0.109 0.109 0 a99 1 0.104 0.072 0.0915 0.095 0.094 0.0882 0.092 0.064 0.0800 0.083 0.078 0.0785 0.080 0.057 0.0720 0.072 0.070 0.0699 0.072

0.051 0.0625 0.065 0.062 0.0625 0.064 0.045 0.0540 0.058 0.056 0.0556 0.056 0.040 0.0475 0.049 0.050 0.0495 0.048 0.036 0.0410 0.042 0.0438 0.0440 0.040 0.032 0.0348 0.035 0.0375 0.0392 0.036

0.0285 0.0317 0.032 0.0344 0.0349 0.032 0.0253 0.0288 0.028 0.0312 0.0313 0.028 0.0226 0.0258 0.025 0.0281 0.0278 0.024 0.0201 0.0230 0.022 0.0250 0.0248 0.022 0.0179 0.0204 0.020 0.0219 0.0220 0.020

0.0159 0.0181 0.018 0.0188 0.0 1 98' 0.018 0.0142 0.0173 0.016 0.0172 0.0175 0.0164 0.0126 0.0162 0.01 4 0.0156 0.0156 0.0148 0.01 13 0.0150 0.013 0.0141 0.0139 0.0136 0.0100 0.0140 0.01 2 0.0125 0.0123 0.0124

0.0089 0.0132 0.010 0.01 09 0.01 10 0.0116 0.0080 0.0128 0.009 0.0102 0.0098 0.0108 0.0071 0.0116 0.008 0.0094 0.0087 0.0100 0.0063 0.0104 0.007 0.0086 o.oon 0.0092 0.0058 0.0095 0.005 0.0078 0.0069 0.00e4

0.0050 0.0090 0.004 0.0070 0.0061 0.0076 0.0045 0.0085 0.0066 0.0054 0.0068 0.0040 0.0080 0.0062 0.0048 0.0060 0.0035 0.0075 0.0043 0.0052 0.0031 0.0070 0.0039 0.0048

0.0066 0.0034 0.0044 0.0062 0 .O03 1 0.0040 0.0060 0.0027 0.0036 0.0058 0.0024 0.0032 0.0055 0.0022 0.0028

0.0052 0.0019 0.0024 0.0050 0.0017 0.0020 0.0048 0.0015 0.0016 0.0048 0.0014 0.0012 0.0062 0.0012 0.0010

METRIC WIRE GAGE is ten times the diameter in millimeccn. I Sometimes u3ed for iron wire. -

TABLE 0-16

CONVERSION TABLES FOR WIRE AND SHEET METAL GAGES

Values in approximate decimals of M inch. As a number of gages BTC in Use for various shapes and metals, it is advisable to state the thickness in thousandths when specifying gage number.

Gage number

0000000 000000 00000 0000 000 00 0

1 2 3 4 5

6 7 8 9 10

11 12 13 14 15

16 17 18 19 20

21 22 23 24 25

26 27 28 29 30

31 32 33 34 35

36 37 38 39 40

41 42 43 44 45

46 47 48 49 50

Gage number

0000000 000000 00000 0000 000 00 0

6 7 8 9

10

11 12 13 14 15

18 17 18 19 20

21 22 23 24 25

26 27 28 29 30

31 32 33 34 35

36 37 38 39 40

41 42 43 44 45

48 47 48 49 50


SECTION 10 RECOMMENDED GOOD PRACTICE

RECOMMENDED GOOD PRACTICE RGP SECTION

This section of the TEMA Standards provides the designer with additional information and guidance relative to the design of shell and tube heat exchangers not covered by the scope of the main sections of the Standards. The title of this section, "Recommended Good Practice", indicates that the information should be considered, but is not a requirement of the basic Standards. When a paragraph in this section (RGP) is followed by an R, C, and/or B, this RGP paragraph is an extension or amplification of a like numbered paragraph in the RCB section of the main Standards. Similarly, other suffix designations following RGP indicate other applicable sections of the main Standards.


RECOMMENDED GOOD PRACTICE SECTION 10

RGP-G-7.11 HORIZONTAL VESSEL SUPPORTS RGP-G-7-11 I LOADS

RGP-G-7.1111 LOADS DUE TO WEIGHT

I

,t I

RVFwr FIXED

SADDLE

RVFwr FIXED

SADDLE

RVSwr SLIDING SADDLE

FIGURE RGP-G-7.1 11 1

1. CALCULATE COMPONENT WEIGHTS AND WEIGHT OF CONTENTS (OPERATING AND TESTING).

2. CALCULATE VERTICAL SADDLE REACTIONS 8 LONGITUDINAL SHELL MOMENTS DUE TO WEIGHT FOR THE EMPTY, OPERATING & TEST CONDITIONS CONSIDERING ACTUAL COMPONENT WEIGHT AND LOCATION.

RVFwr = VERTICAL REACTION @ FIXED SADDLE DUE TO WEIGHT RVSwr = VERTICAL REACTION @ SLIDING SADDLE DUE TO WEIGHT SMFwr = LONGITUDINAL SHELL MOMENT @ FIXED SADDLE DUE TO WEIGHT SMSwr = LONGITUDINAL SHELL MOMENT @ SLIDING SADDLE DUE TO WEIGHT SMMwr = MAXIMUM LONGITUDINAL SHELL MOMENT BETWEEN SADDLES DUE TO WEIGHT

RGP-G-7.1112 EARTHQUAKE FORCES

I RVSwr

SLIDING SADDLE

W MSFEa

FIXED SADDLE

RVFEa RVSEa

I L d

FIXED SLIDING SADDLE SADDLE

FIGURE RGP-G-7.1112

1. CALCULATE SEISMIC REACTIONS AND MOMENTS.

RHSEa = RHFw x CS M S k a = RHFm x H MSSEa = RHSEo x H

Cs = SEISMIC FACTOR RLFEo = TOTAL EXCH WT x Cs RLSEa = 0 (SLIDING SADDLE) SMFECI = SMFwr x Cs SMSEa = SMSwr x Cs

SMMEQ = SMMwr x Cs RVFEa = (RLFm x H) / L RVSEa = (RLFEa x H) I L RHFEa = RVFw x Cs

p/ MSSEQ

SLIDING SADDLE


RGP-G-7.1113 WIND LOADS

FIXED RVFw RVSw SADDLE FIXED SLIDING

SADDLE SADDLE

W MSSw

SLIDING SADDLE

FIGURE RGP-G-7.1113

1. CALCULATE WIND LOADS (CALCULATE TOTAL WIND FORCE). FLw = WEFF x HEFF x EFFECTIVE WIND LOAD (AS DETERMINED BY APPROPRIATE CODE) FHw = HEFF x LEFF x EFFECTIVE WIND LOAD (AS DETERMINED BY APPROPRIATE CODE) RLFw = FLw (MAY BE CONSIDERED NEGLIGIBLE FOR SMALL EXCHANGERS) RLSw = 0 (SLIDING SADDLE) SMFw = LONGITUDINAL SHELL MOMENT @ FIXED SADDLE DUE TO TRANSVERSE WIND

(SHELL MOMENT DUE TO LONGITUDINAL WIND MAY BE CONSIDERED NEGLIGIBLE) SMSw = LONGITUDINAL SHELL MOMENT @ SLIDING SADDLE DUE TO TRANSVERSE WIND

(SHELL MOMENT DUE TO LONGITUDINAL WIND MAY BE CONSIDERED NEGLIGIBLE) SMMw = MAXIMUM LONGITUDINAL SHELL MOMENT BETWEEN SADDLES DUE TO TRANSVERSE WIND

(SHELL MOMENT DUE TO LONGITUDINAL WIND MAY BE CONSIDERED NEGLIGIBLE)

RVFw = (RLFw x HEFF/~) / L RVSw = (RLFw x HEFF/~) / L RHFw = FHw x ((A + 0.5L) I LEFF)

RHSw = FHw x ((B + 0.5L) I LEFF) MSFw = RHFw x HEFF/~ MSSw = RHSw x HEW/;!

RGP-G-7.1114 THERMAL EXPANSION LOADS LOADS CAUSED BY LONGITUDINAL GROWTH BETWEEN FIXED & SLIDING SADDLES

c:t FIXED

SADDLE

---P I - SMFw. SMMw. SMSw,

- f - -

FIXED SLIDING SADDLE SADDLE

FIGURE RGP-G-7.1114

SLIDING SADDLE

1. CALCULATE LOADS DUE TO THERMAL EXPANSION (WHERE p = COEFFICIENT OF FRICTION BETWEEN FOUNDATION AND BASE PLATE AT SLIDING SADDLE).

RLFw = RVSw x p. RLSEXP = RVSw x p SMFw = RLFw x H

SMSw = RLSw x H SMMw = RLSw x H p FOR STEEL = 0.8 p FOR LUBRICATED PLATE = 0.1


R P

RGP-G-7.1115 COMBINED FORCES

MSFEFF FIXED

SADDLE

SMFEFF SMMEFF

S

RLSEFF RHSEFF 4 RVFEFF FIXED

SADDLE

RVSEFF SLIDING SADDLE

MSSEFF SLIDING SADDLE

FIGURE RGP-G-7.1115

1. CALCULATE THE COMBINED SADDLE REACTIONS FOR THE FOLLOWING CASES OR AS APPROPRIATE IN DESIGN CRITERIA:

DEAD WEIGHT EMPTY DEAD WEIGHT EMPTY + EARTHQUAKE DEAD WEIGHT OPERATING DEAD WEIGHT OPERATING + EARTHQUAKE DEAD WEIGHT FLOODED DEAD WEIGHT FLOODED + EARTHQUAKE DEAD WEIGHT EMPTY + WIND DEAD WEIGHT OPERATING + THERMAL EXPANSION DEAD WEIGHT OPERATING + WIND OR ANY OTHER APPROPRIATE COMBINATION DEAD WEIGHT FLOODED +WIND

2. CALCULATE RESULTANT SADDLE LOAD 8, SHELL MOMENT FOR WINDIWRTHQUAKE CASES: RVFEFF = LARGER OF (RVFW~+ RHFW~I'' OR ( R V F ~ ~ + RHFEQ~ 1'" RVSEFF = LARGER OF (RVSw2+ RHSw2y" OR (RVSw2+ RHSEa')'' SMFEFF = LARGER OF (SMFw2+ SMFW'~" OR (SMFw2+ SMFEa2)lR SMSEFF = LARGER OF (SMSw'+ SMSw2YR OR (SMSw2+ SMSEO' >'" SMMEFF = LARGER OF (SMMw2+ SMMwZ)'' OR (SMMw2+ SMMEa2)'"

RGP-G-7.1116 EFFECTIVE REACTION LOAD SADDLE ANGLE

ACTUAL SADDLE ANGLE

EFFECTIVE SADDLE ANGLE

FIGURE RGP-G-7.1116 1. CALCULATE THE EFFECTIVE SADDLE ANGLE FOR EACH SADDLE FOR ALL WIND AND EARTHQUAKE CASES.

2. EFFECTIVE SADDLE ANGLE = ((ACTUAL SADDLE ANGLE DIVIDED BY 2 ) - ARCTAN(RH/RV)) X 2 (SEE FIGURE RGP-G-7.1116). ._



RGP-G-7.112 STRESSES

ONCE THE LOAD COMBINATIONS HAVE BEEN DETERMINED, THE STRESSES ON THE EXCHANGER CAN BE CALCULATED. THE METHOD OF CALCULATING STRESSES IS BASED ON "STRESSES IN LARGE HORIZONTAL CYLINDRICAL PRESSURE VESSfLS ON TWO SADDLE SUPPORTS", PRESSURE VESSEL AND PIPING: DESIGN AND ANALYSIS, ASME, 1972, BY L.P. ZICK

7 Sin = LONGITUDINAL STRESS AT SADDLE WITH STIFFENER 7 SI' = LONGITUDINAL STRESS AT SADDLES

(TENSION AT TOP, COMPRESSION AT BOTTOM)

- I!---- I I {'- - + - -'+ + -Tt -\++ ?;$;- - - - - - - - - -

LS,= CIRCUMFERENTIAL COMPRESSION AT BOTTOM OF SHELL I h AT MIDSPAN

S, = TANGENTIAL SHEAR IN HEAD

L S3 = CIRCUMFERENTIAL STRESS AT HORN OF SADDLE

S2 = TANGENTIAL SHEAR - RESULTS IN DIAGONAL LINES IN SHELL

FIGURE RGP-G-7.112


RECOMMENDED GOOD PRACTICE

RGP-G-7.1121 LONGITUDINAL STRESS AT MID SPAN (SI)

LONGITUDINAL STRESS LONGITUDINAL STRESS (METRIC)

WHERE

SMMEFF = MAXIMUM EFFECTIVE SHELL MOMENT AT

r = OUTSIDE SHELL RADIUS, inches (rnrn) ts = SHELL THICKNESS, inches (rnrn)

MID SPAN (SEE FIGURE RGP-G-7.1115) in-lb (rnrn-kN)

RGP-G-7.1122 LONGITUDINAL STRESS AT THE SADDLE WITHOUT STIFFENERS (Si')

THIS AREA IS INEFFECTIVE AGAINST LONGITUDINAL BENDING IN AN UNSTIFFENED SHELL

t

SECTION 10


- - kPa SMFEFF or SMSEFF .

SIN2A A + SINACOSA - 2 7

WHERE

- -v - * 4

SMFEFF , SMSEFF = MAXIMUM EFFECTIVE SHELL MOMENT AT FIXED

r = OUTSIDE SHELL RADIUS, inches (rnrn) ts = SHELL THICKNESS, inches (rnrn) A = % EFFECTIVE SADDLE ANGLE, radians

OR SLIDING SADDLE (SEE FIGURE RGP-G-7.1115) in-lb, (rnrn-kN)

d - l EFFECTIVE SECTION MODULUS OF ARC


RGP-G-7.1123 LONGITUDINAL STRESS AT THE SADDLE WITH STIFFENER RINGS OR END CLOSURES CLOSE ENOUGH TO SERVE AS STIFFENERS (Sin)


s; = f ( zr2 ts ) ,06 , kPa SMFEFF Or SMSEFF SMFEFF or SMSEFF Ib S1" = f

WHERE

SMFEFF , SMSEFF = MAXIMUM EFFECTIVE SHELL MOMENT AT FIXED

r = OUTSIDE SHELL RADIUS, inches (rnrn) ts = SHELL THICKNESS, inches (rnm)

IF THE SHELL IS STIFFENED IN THE PLANE OF THE SADDLE OR ADJACENT TO THE SADDLE OR THE SADDLE IS WITHIN A 5 1-12 OF THE END CLOSURE, THEN THE ENTIRE SECTION MODULUS OF THE CROSS SECTION IS EFFECTIVE.

OR SLIDING SADDLE (SEE FIGURE RGP-G-7.1115) in-lb, (rnm-Wu) SECTION MODULUS = X r z ts . inches3 (mm3)

ALLOWABLE STRESS LIMIT FOR Si, Si' 8 Si"

TENSION - THE TENSILE STRESS + THE LONGITUDINAL STRESS DUE TO PRESSURE TO BE LESS THAN THE ALLOWABLE TENSION STRESS OF THE MATERIAL AT THE DESIGN TEMPERATURE TIMES THE JOINT EFFICIENCY OF THE GIRTH JOINT

FACTOR IN THE CODE FOR LONGITUDINAL COMPRESSION OF THE MATERIAL AT THE DESIGN TEMPERATURE.

COMPRESSION - THE COMPRESSIVE STRESS IS TO BE LESS THAN THE B



120" 1.171, 130" 1.022 140" 0.900 150" 0.799

RGP-G-7.1124 TANGENTIAL SHEAR STRESS IN PLANE OF SADDLE (SZ)

A) UNSTIFFENED SHELL

r

TANGENTIAL SHEAR STRESS

~(RVFEFF or RVSEFF) Ib s2 = rtS ' in2

-

-

RVFEFF or RVSEFF

SECTION 10

TANGENTIAL SHEAR STRESS (METRIC)

x lo', kPa KZ(RVFEFF or RVSEFF)

rts s2 =

MAXIMUM SHEAR AT 8 =a

WHERE

RVFEFF , RVSEFF = MAXIMUM EFFECTIVE RESULTANT SADDLE LOAD AT FIXED

8, degrees OR SLIDING SADDLE (SEE FIGURE RGP-G-7.1115) in-lb, (mm-kN)

p = (180 - 8 ), degrees

8 a = li - &( ?+ &) , radians

r = OUTSIDE SHELL RADIUS, inches (mm) ts = SHELL THICKNESS, inches (mm)

SINa K2 = x-a + SINaCOSa

CONSTANT Kz FOR VARIOUS VALUES OF 8

I e I & I

B) SHELL STIFFENED BY RINGS IN PLANE OF SADDLE

STIFFENING RING

TANGENTIAL SHEAR STRESS TANGENTIAL SHEAR STRESS (METRIC)

~(RVFEFF or RVSEFF) Ib 106, kPa s2 =

KZ(RVFEFF or RVSEFF) rts

- s2 = rtS ' in2

WHERE

RVFEFF , RVSEFF = MAXIMUM EFFECTIVE RESULTANT SADDLE LOAD AT FIXED

r = OUTSIDE SHELL RADIUS, inches (mm) ts = SHELL THICKNESS, inches (mm) K2 = = .318

OR SLIDING SADDLE (SEE FIGURE RGP-G-7.1115) in-lb, (mm-kN)



C) SHELL STIFFENED BY END CLOSURE (A 5 r/2)

TANGENTIAL SHEAR STRESS

~(RVFEFF Or RVSEFF) Ib s2 = rts ' 3

MAXIMUM SHEAR AT 8 = a

WHERE

TANGENTIAL SHEAR STRESS (METRIC)

~(RVFEFF or RVSEFF) , kpa s2 = rts

RVFEFF , RVSEFF = MAXIMUM EFFECTIVE SHELL MOMENT AT FIXED OR SLIDING SADDLE (SEE FIGURE RGP-G-7.1115) in-lb, (mm-kN)

8, degrees

p = (180 - 1 ), degrees

a = x -&(! +&) ,radians

r = OUTSIDE SHELL RADIUS, inches (mm) ts = SHELL THICKNESS, inches (mm)

SlNa a-SINaCOSa ~2 = x [ z-a + SiNaCOSa]

ALLOWABLE STRESS LIMIT -

CONSTANT K2 FOR VARIOUS VALUES OF 8

THE MAXIMUM TANGENTIAL SHEAR STRESS FOR CASES A, B, 8 C IS TO BE LESS THAN 0.8 TIMES THE MAXIMUM ALLOWABLE STRESS IN TENSION OF THE SHELL MATERIAL AT THE DESIGN TEMPERATURE.



RGP-G-7.1125 CIRCUMFERENTIAL STRESS AT HORN OF SADDLES UNSTIFFENED (S3)

SECTION 10

I

CIRCUMFERENTIAL STRESS AT HORN OF SADDLE

FOR Ls 2 8r 3ffi(RVFEFF OR RVSEFF) k - 2ts2 1 in*

RVFEFF OR RVSEFF) s3 = - ( 4ts(b + lots)

OR

FOR Ls < 8r (RVFEFF OR RVSEFF) k r(RVFEFF OR RVSEFF) &

s3 = - 4ts(b + lots) Lsts 2 I in2 -

CIRCUMFERENTIAL STRESS AT HORN OF SADDLE (METRIC)

FOR Ls 2 8r 3K3(RVFEFF OR RVSEFF) - x to6, Wa

2ts2 1 RVFEFF OR RVSEFF) s3= [ ( 4ts(b+ lots)

OR

FOR Ls < 8r RVFEFF OR RVSEFF) ffi T(RVFEFF OR RVSEFF) - 1 x 10" kPa

s3= ( 4ts(b + lots) Lsts 2 L -1

WHERE

RVFEFF, RVSEFF = MAXIMUM EFFECTIVE VERTICAL REXCTION AT THE FIXED AND SLIDING SADDLE RESPECTIVELY, Ib (kN)

r = OUTSIDE SHELL RADIUS, inches (rnm) b =WIDTH OF SADDLE, inches (rnrn)

Ls = SHELL LENGTH BETWEEN TUBESHEETS OR BETWEEN SHELL FLANGES OR BETWEEN SHELL FLANGE TO HEAD TANGENT LINE, inches (mm)

ffi = CONSTANT FROM FIGURE RGP-G-7.1125

MAXIMUM ALLOWABLE STRESS LIMIT FOR S3 = 1.25 TIMES ALLOWABLE STRESS IN TENSION FOR THE SHELL MATERIAL AT DESIGN TEMPERATURE. -


ENDED GOO TlCE

Figure RGP-G-7.1125 VALUE OF CONSTANT &

A = Distance from tubesheet or shell flange or head tangent line to center of saddle, inches (-1 r = Outside radius of shell, inches (mm)

RATIO Alr



120'

SECTION 10

0.401

RGP-G-7.1126 STRESS IN HEAD USED AS STIFFENER ( S , )

1 I

130' I 0.362 140' I 0.327

If the head stiffness is used by locating the saddle close to the head, tangential shear stress should be added to the head pressure stress. The tangential shear has horizontal components which cause tension across the head.

Central Angle a = 5~ - -(- + p), radians 180 2 20

p = (180 - W2), degrees

8 Ln - a + sin a cosaJ

9, degrees

Constant & Value For Various Saddle Contact Angles, 8

I 150' I 0.297 I I

s4 =

Where t, = thickness of head, inches(m)

Allow- . .

The tangential shear is to be combined with the pressure stress in the head and should be less than 1.25 times the maximum allowable stress in tension of the head material at design temperahln-



RGP-G-7.1127 RING COMPRESSION IN SHELL OVER SADDLE (S5)

8 120' 130'

The s u m of the tangential forces on both sides of the saddle at the shell band causes a ring compression stress in the she11 band. A width of shell equal to 5ts each side of the saddle plus the saddle width resists this force. Wear plates of greater width than the saddle may be used to reduce the stress.

K5 0.760 0.726

ts

P Central Angle a = x - -(- + -),radians 180 2 20

1 + cos a 11c - a + sinacosct K.5 =

Constant Ks Value For Various Saddle Contact Angles, 8

I

I 1 40" I 0.697 I I

t 150' I 0.673 I - .

1

Ring Compression Stress

(RVF, or RVSa,) IS5 1b s, = 7 -

ts(b + lots) in*

Where b = saddle width, inches(rnm)

Ring Cornmession Stress (Metric)

ts(b + lots)

. . able S t r w The maximum compressive stress should be less than 0.5 times the yield stress of the material at the design temperature. This should not be added to the pressure stress.


RECOMMENDED G D PRACTICE SECTION 10

RGP-G-7.113 DESIGN OF SADDLE PARTS

DETERMINE MAXIMUM LOADS FROM APPLICABLE LOAD CONDlnON SEE FIGURE RGP-G-7.1115

~

-RHFEFF MSFEFF . .-a___ RHSEFF

L-J-RLFEFF R LSEFF

t M b b E F F

RVFEFF RVSEFF

THERE ARE MANY TYPES OF BASE PLATE, WEB & GUSSET ARRANGEMENTS. THE FOLLOWING APPROACH IS OFFERED AS ONE OF MANY.

WEB

\SADDLE CENTROID ARC- OF

-1- - - - -1. - * - - I I

WEB Z

~ GUSSET

LBASE PLATE

CALCULATE PROPERTIES OF SADDLE ABOUT X - X & Z - z AXIS

A=AREA, inz(mmz ) I x - x , Iz-z=MOMENT OF INERTIA ABOUT x - x OR z - z , in4 (mm4 1 S x - x , Sz-z=SECTION MODULUS ABOUT x - x OR z - z . inJ(mrnJ 1

CHECK WEB & GUSSETS AS COMBINED CROSS-SECTION FOR BENDING

BENDING STRESS ABOUT BENDING STRESS ABOUT X - x AXIS x-x AXIS (METRIC)

X lo6, kPa Mx-x s x - x

Sb =

WHERE M x - x =(RLFEFF OR RLSEFF) X ~ E F F , in-lb (mm-kN) Sb < 90% YIELD STRESS

BENDING STRESS ABOUT Z-z AXIS

BENDING STRESS ABOUT Z - z AXIS (METRIC)

-

WHERE Mz-z = (MSFEFF OR MSSEFF), in-lb (mm-kN) Sb < 90Z YIELD STRESS


CHECK WEB & GUSSETS AS COMBINED CROSS-SECTION FOR COMPRESSION

STRESS IN COMPRESSION, RVFEFF or RVSEFF & A ’ in2 sc =

RVFEFF or RVSm (wa) STRESS IN COMPRESSION, Sc = A

STRESS LIMIT = ALLOWABLE COMPRESSIVE STRESS

COMBINE STRESS FROM BENDING AND COMPRESSION

I 1 ACTUAL COMPRESSIVE STRESS ALLOWABLE COMPRESSIVE STRESS

ACTUAL BENDING STRESS + ALLOWABLE BENDING STRESS



P 7~ t P-c: /) -1

bw * .a I-

RGP-G-7.42 VERTICAL VESSEL SUPPORTS THE VESSEL LUGS DESCRIBED IN THIS PARAGRAPH INCORPORATE TOP PLATE, BASE PLATE AND TWO GUSSETS. OTHER CONFIGURATIONS AND METHODS OF CALCULATIONS ARE ACCEPTABLE.

Ht = DISTANCE BETWEEN TOP PLATE AND BOTTOM PLATE, inches (mm)

Tb = THICKNESS OF BOTTOM PLATE, inches (mm) Tt = THICKNESS OF TOP PLATE, inches (mm) Tg = THICKNESS OF GUSSETS, inches (mm) TP = TOP PLATE WIDTH, inches (mm) GB = BOTTOM PLATE WIDTH, inches (mm) bw = BEARING WIDTH ON BASE PLATE

' ,_I

APPLIED LOADS

r I W

I I 1

I I I

f TENSION

LOAD UPLIFT

L - - & I I

I 4M dBN

I I I I

I

I dB

I

W = TOTAL DEAD WT. PER CONDITION ANALYZING (EMPTY, OPERATION, FULL OF WATER, ETC...), Ib (kN)

N = NUMBER OF LUG SUPPORTS dB = BOLT CIRCLE, inches (mm) M = OVERTURNING MOMENT AT THE SUPPORTS

DUE TO EXTERNAL LOADING, in-lb (mm-kN) 4M W

MAXTENSION = - - - , Ib (H) (UPLIFT) dBN N

I F W > - 4M NO UPLIFT EXISTS dB

4M W dBN N

MAX COMPRESSION = - + - , Ib (W)

TOTAL COMP. LOAD

c

RGP-G-7.121 DESIGN OF VESSEL SUPPPORT LUG

P= LL EC , Ib (kN) Ht

k:d Standards Of The Tubular Exchanger Manufacturers Association 267

SECTION 10 RECOMMENDED GOOD PRACTICE RGP-G-7.122 BASE PLATE CONSIDER BASE PLATE AS A SIMPLY SUPPORTED BEAM SUBJECT TO A

UNIFORMLY DISTRIBUTED LOAD w, Ib (kN)

Q + 2Tg

o(Q+Tg)2 , in-lb (mm-kN) 8 MB =

WHERE

FOR TENSION DUE TO UPLIFT, CONSIDER BASE PLATE AS SIMPLY SUPPORTED BEAM WITH A CONCENTRATED LOAD LL, Ib (kN) AT ITS CENTER

bw

LL(Q+ Tg) , in-lb (mrn-kN) 4

BENDING STRESS BENDING STRESS (METRIC)

1 LI: ~ MT=

Ib 6M * - (bw)frb)’ ’ in2 Sb = 6M* x 109 kPa

(bW)Crb)* Sb =

Sb c 90% YIELD STRESS

M* = GREATER OF ME OR M i

RGP-G-7.123 TOP PLATE ASSUME SIMPLY SUPPORTED BEAM WITH UNIFORM LOAD

+ w

RGP-G-7.124 GUSSETS

tv ’i?

, in-lb (rnm-kN) w(Q + TgI2

8 M =

WHERE P

BENDING STRESS BENDING STRESS (METRIC)

Ib - 6M (TPt2x frt) ’ in2

Sb =

Sb c 90% YIELD STRESS

GB Tp , degrees Ht

a =ARCTAN

e = eccentricity = EC - - , inches (mm) GB 2

MAX. COMPRESSIVE STRESS AT B MAX. COMPRESSIVE STRESS AT B (METRIC)

6e GB x Tg x (COS a)2 + )’ in2 sc = GB x Tg x (COS a)2 GB x ( 1 +-)x106, kPa LL 12 6e Ib LL R sc =

Sc c THE ALLOWABLE STRESS IN COMPRESSION (COLUMN BUCKLING PER AISC)



P

L

RGP-GJ.2 LIFTING LUGS (SOME ACCEPTABLE TYPES OF LIFTING LUGS) RGP-G-7.21 VERTICAL UNITS

SECTION 10

COVER LUG

~ t

I

TAILING LUG



RGP-G-7.22 HORIZONTAL UNITS

SLING LIFT PREFERRED METHOD OF LIFTING IS SLINGING

CG I I u

SHELL ERECTION LUGS ONLY IF SPECIFIED BY CUSTOMER

RGP-G-7.23 TYPICAL COMPONENT LIFTING DEVICES

EYE BOLT LIFTING LUG



RGP-G-7.24 LIFT PROCEDURE

1. ESTABLISH LlFF PROCEDURE. LIFT PROCEDURE IS ESTABLISHED BY CUSTOMER. THIS STEP MAY NOT BE NECESSARY FOR ROUTINE LIFTS.

EXAMPLE :

SECTION 10

TOTAL WEIGHT

I

I 1 4 I

SPREADER BEAM

- CABLES TO BE E P T VERTICAL I

SLING OR TAIL LUG ADJACENT TO BASE RING

2. CALCULATE WEIGHT TO BE LIFIED.

3. APPLY IMPACT FACTOR. 1.5 MINIMUM, UNLESS OTHERWISE SPECIFIED.

4. SELECT SHACKLE SIZE. NO IMPACT FACTOR IS APPLIED UNLESS CUSTOMER SPECIFIED. SHACKLE TABLES ARE AVAILABLE FROM SHACKLE MANUFACTURERS.

5. DETERMINE LOADS THAT APPLY (SEE ABOVE FIGURES).


6. SIZE LIFTING LUG. THICKNESS OF LIFTING LUG IS CALCULATED BY USING THE GREATER OF SHEAR OR BENDING RESULTS AS FOLLOWS:

P

r A I

P

Itt-

t = REQUIRED THICKNESS OF LUG, inches (mm)

Sb = ALLOWABLE BENDING STRESS OF LUG, psi (kPa)

S = ALLOWABLE SHEAR STRESS OF LUG, psi (kPa)

L =WIDTH OF LUG. inches (mm) h = DISTANCE, CENTERLINE OF HOLE TO COMPONENT, inches (mm) p = DESIGN LOAD / LUG INCLUDING IMPACT FACTOR, Ib. (kN)

r = RADIUS OF LUG, inches (mm) d = DIAMETER OF HOLE, inches (mm)

REQUIRED THICKNESS FOR SHEAR REQUIRED THiCKNESS FOR SHEAR (METRIC)

P P x l o 6 ,mm t = , inches t = 2(S)(r - d/2) 2(S)(r - d/2)

REQUIRED THICKNESS FOR BENDING REQUIRED THICKNESS FOR BENDING (METRIC)

6 P h t = , inches

Sb(L)2

6 x 10 ,mm 6 P h

Sb(L)2 t =

USE GREATER OF THICKNESS REQUIRED FOR BENDING OR SHEAR.

NOTE: COMPONENT SHOULD BE CHECKED AND/OR REINFORCED FOR LOCALLY IMPOSED STRESSES.



RGP-G-7.3 WIND AND SEISMIC DESIGN For purposes of design, wind and seismic forces are assumed to be negligible unless the purchaser specifically details such forces in the inquiry. When such requirements are specified by the purchaser, the designer should consider their effects on the various components of the heat exchanger. These forces should be evaluated in the design of the heat exchanger for the pressure containing components, the heat exchanger supports and the device used to attach the heat exchanger supports to the anchor points. Methods used for the design analysis are beyond the scope of these Standards; however, the designer can refer to the selected references listed below. References: (1) ASME Boiler and Pressure Vessel Code, Section Ill, "Nuclear Power Plant Components.'' (2) "Earthquake Engineering", R. L. Weigel, Prentice Hall, Inc., 1970. (3) "Fundamentals of Earthquake Engineering", Newark and Rosenbluth, Prentice Hall, Inc., 1971. (4) Steel Construction Manual of the American Institute of Steel Construction, Inc., 8th Edition. (5) TID-7024 (1963), "Nuclear Reactors and Earthquakes", U.S. Atomic Energy Commission Division

(6) "Earthquake Engineering for Nuclear Reactor Facilities (JAB-101 )", Blume, Sharp and Kost, John

(7) "Process Equipment Design", Brownell and Young, Wiley and Sons, Inc., 1959.

of Technical Information.

A. Blume and Associates, Engineers, San Francisco, California, 1971.

RGP-RCB-2 PLUGGING TUBES IN TUBE BUNDLES In U-tube heat exchangers, and other exchangers of special design, it may not be possible or feasible to remove and replace defective tubes. Under certain conditions as indicated below, the manufacturer may plug either a maximum of 1 % of the tubes or 2 tubes without prior agreement. Condition: (1) For U-tube heat exchangers where the leaking tube(s) is more than 2 tubes away from the periphery of

the bundle. (2) For heat exchangers with limited access or manway openings in a welded-on channel where the tube is

located such that it would be impossible to remove the tube through the access opening in the channel. (3) For other heat exchanger designs which do not facilitate the tube removal in a reasonable manner. (4) The method of tube plugging will be a matter of agreement between manufacturer and purchaser. (5) The manufacturer maintains the original guarantees. (6) "As-built" drawings indicating the location of the plugged tube(s) shall be furnished to the purchaser



RGP-RCB-4.62 SHELL OR BUNDLE ENTRANCE AND EXIT AREAS This paragraph provides methods for determining approximate shell and bundle entrance areas for common configurations as illustrated by Figures RGP-RCB-4.6211, 4.621 2, 4.6221, 4.6222, 4.6231 and 4.6241. Results are somewhat approximate due to the following considerations:

1 Non-uniform location of tubes at the periphery of the bundle. I1 2 The presence of untubed lanes through the bundle. (3) The presence of tie rods, spacers, and/or bypass seal devices.

Full account for such concerns based on actual details will result in improved accuracy. Special consideration must be given to other configurations. Some are listed below:

1 Nozzle located near the bends of U-tube bundles. I 1 2 Nozzle which is attached in a semi or full tangential position to the shell. (3) Perforated distribution devices. (4) Impingement plates which are not flat or which are positioned with significant clearance off

the bundle. (5) Annular distributor belts.

RGP-RCB-4.621 AND 4.622 SHELL ENTRANCE OR EXIT AREA The minimum shell entrance or exit area for Figures RGP-RCB-4.6211,4.6212, 4.6221 and 4.6222 may be approximated as follows:

where A = Approximate shell entrance or exit area, inches 2 (mm 2).

D = Nozzle inside diameter, inches (mm)

h = Average free height above tube bundle or impingement plate, inches (mm)

h = 0.5 ( h + h

h = 0 . 5 ( D s - O T L )

for Figures RGP-RCB-4.6211,4.6212 and 4.6222.

for Figure RGP-RCB-4.6221.

h = Maximum free height (at nozzle centerline), inches (mm)

h = Minimum free height (at nozzle edge), inches (mm)

h = h - 0.5 [ D - ( D 2- D 2 ) 0 ” ]

D = Shell inside diameter, inches (mm)

O T L = Outer tube limit diameter, inches (mm)

F , = Factor indicating presence of impingement plate

F = 0 with impingement plate

F , = 1 without impingement plate



P =Tube center to center pitch, inches (mrn)

D =Tube outside diameter, inches (rnm)

F = Factor indicating tube pitch type and orientation with respect to fluid flow direction

F 2 =I.Ofor and

F = 0.866 for + F 2 =0.707 for

RGP-RCB-4.623 AND 4.624 BUNDLE ENTRANCE OR EXIT AREA The minimum bundle entrance or exit area for Figures RGP-RCB-4.6231 and 4.6241 may be approximated as follows:

where A b = Approximate bundle entrance or exit area, inches B = Baffle spacing at entrance or exit, inches (mrn)

(rnrn 2).

K = Effective chord distance across bundle, inches (rnm)

K = D ,, for Figure RGP-RCB-4.6231

A = Area of impingement plate, inches 2 (rnm 2)

A , =O for no impingement plate 2

A p = - for round impingement plate 4

A , = I , 2 for square impingement plate

I = Impingement plate diameter or edge length, inches (mrn)

A = Unrestricted longitudinal flow area, inches 2 (rnm 2)



The formulae below assume unrestricted longitudinal flow. A = 0 for baffle cut normal to nozzle axis

A = 0.5a b for Figure RGP-RCB-4.6231 with baffle cut parallel with nozzle axis

A = 0.5 ( D - 0 T L ) c for Figure RGP-RCB-4.6241 with baffle cut parallel with nozzle axis

Q = Dimension from Figure RGP-RCB-4.6231, inches (mm)

b = Dimension from Figure RGP-RCB-4.6231, inches (mm)

c = Dimension from Figure RGP-RCB-4.6241, inches (mm)

RGP-RCB-4.625 ROD TYPE IMPINGEMENT PROTECTION Rod type impingement protection shall utilize a minimum of two rows of rods arranged such that maximum bundle entrance area is provided without permitting direct impingement on any tube. Shell entrance area may be approximated per Paragraph RGP-RCB-4.622, Figure

Bundle entrance area may be approximated per Paragraph RGP-RCB-4.624, Figure RGP-RCB-4.6221.

RGP-RCB-4.6241.


D PRACTICE SECT

FIGURES RGP-RCB-4.6211 4.6212,4.6221 AND 4.6222

SHELL ENTRANCE OR EXIT AREA

FIGURE RGP- RCB- 4.621 I IMPINGEMENT PLATE -L FULL LAYOUT I

on h2 hl I I

I h2 h:

I 1

I FIGURE RGP- RC8-4.6221 NO IMPINGEMENT PLATE - FUU LAYOUT

FIGURE RGP - RCB - 4.6212 IMPINGEMENT PLATE - PARTIAL LAYOUT

FIGURE NO IMPINGEMENT PLATE - MRTIAL LAYOUT

RGP - RCB - 4.6222

( 0,- O T U 2


FIGURES RGP-RCB-4.6231 AND 4.6241

BUNDLE ENTRANCE OR EXIT AREA

FIGURE RGP-RCB-4.6231 PARTIAL LAYOUT- WITH OR WITHOUT IMPINGEMENT PLATE

3-

VlEWI'A A"

I I

FIGURE RGP - RCB - 4,624 1; FULL LAYOUT - NO IMPINGEMENT PLATE

(0 , -OTL)/2 I



RGP-RCB-6 GASKETS RGP-RCBB.l TYPE OF GASKETS Gaskets made integral by welding are often harder in the welds than in the base material. Hardness limitations may be specified by the exchanger manufacturer.

RGP-RCB-7 TUBESHEETS

RGP-RCB-7.2 SHELL AND TUBE LONGITUDINAL STRESSES, FIXED TUBESHEET EXCHANGERS

The design of fixed tubesheets in accordance with Paragraph RCB-7.16 is based, in part, upon the tube bundle providing elastic support to the tubesheets throughout the tubed area. It is therefore important to insure that the tubes can provide sufficient staying action against tensile forces and sufficient stability against compressive forces. Paragraph RCB-7.2 provides rules to calculate the tube loads at the periphery of the bundle only. The tubes at the interior of the bundle are not considered, but can become loaded both in tension and compression. Tensile forces are generally not a problem if the requirements of Paragraph RCB-7.2 are met. Compressive forces might, however, create unstable conditions for tubes at the interior of the bundle. Typical conditions that can cause this are: Loading :

Geometry:

Methods similar to those provided in the following references can be used to predict loadings on the tubes at the interior of the bundle:

(1) Gardner, K.A., "Heat Exchanger Tubesheet Design", Trans. ASME, Vol. 70, 1948, pp. A-377-385. (2) Gardner, K.A., "Heat Exchanger Tubesheet Design-2: Fixed Tubesheets", Trans. ASME, Vo1.74,

(3) Miller, K.A.G., "Design of Tube Plates in Heat Exchangers", Proc. Inst. Mech. Eng., Ser. B, Vol. 1,

(4) Yu, Y.Y., "Rational Analysis of Heat-Exchanger Tube-Sheet Stresses", Trans. ASME, Vol. 78, 1956, pp. A-468-473.

(5) Boon, G.B. and Walsh, R.A., "Fixed Tubesheet Heat Exchangers", Trans. ASME, Vol. 86, Series E, 1964, pp. 175-180 (See also Gardner, K.A., discussion of above, Trans. ASME, Vol. 87, 1965,

Tube side pressure and/or differential thermal expansion where the shell, if unrestrained, would lengthen more than the tubes. (Positive P d per Paragraph

Flexible tubesheet systems. Generally, those that are simply supported at the edge (F = 1 per Paragraph RCB-7.132) and have a value of F (Paragaph RCB-7.161) greater than 2.5.

RCB-7.161)

1952, pp. A-159-166.

1952, pp. 215-231.

pp. 235-236). (6) Gardner, K.A., 'Tubesheet Design: A Basis For Standardization", Proceedings of the First

International Conference on Pressure Vessel Technology: Part 1, Design and Analysis, pp- 621-648 and Part Ill, Discussion, pp. 133-135, ASME, 1969 and 1970.

(7) Chiang, C.C., "Close Form Design Solutions for Box Type Heat Exchangers", ASME 75-WA/DE-15.

(8) Hayashi, K., "An Analysis Procedure for Fixed Tubesheet Exchangers", Proceedings of the Third International Conference on Pressure Vessel Technology: Part 1, Analysis, Design and Inspection, pp. 363-373, ASME, 1977.

1977. (9) Malek, R.G., "A New Approach to Exchanger Tubesheet Design", Hydrocarbon Processing, Jan.

(10) Sin h, K.P., "Anal sis of Vertically Mounted Through-Tube Heat Exchangers", ASME

The allowable tube stresses and loads presented in Paragraph RCB-7.2 are intended for use with an analysis considering only the peripheral tubes. These allowable stresses and loads can be modified if the tubes at the interior of the bundle are included in the analysis. Engineering judgement should be used to determine that the bundle can adequately stay the tubesheets against tensile loadings and remain stable against compressive loadings.

77 19 PGC-NE-19, Y rans. ASME, Journal of Engineering for Power, 1978.



RGP-RCB-7.4 TUBE HOLES IN TUBESHEETS

RGP-RCB-7.43 TUBE HOLE FINISH Tube hole finish affects the mechanical strength and leak tightness of an expanded tube-to-tubesheet joint. In general: (1) A rough tube hole provides more mechanical strength than a smooth tube hole. This is

influenced by a complex relationship of modulus of elasticity, yield strength and hardness of the materials being used.

(2) A smooth tube hole does not provide the mechanical strength that a rough tube hole does, but it can provide a pressure tight joint at a lower level of wall reduction.

(3) Very light wall tubes require a smoother tube hole finish than heavier wall tubes. (4) Significant longitudinal scratches can provide leak paths through an expanded

tube-to-tubesheet joint and should therefore be removed.

RGP-RCB-7.5 TUBE WALL REDUCTION The optimum tube wall reduction for an expanded tube-to-tubesheet joint depends on a number of factors. Some of these are: (1) Tube hole finish (2) Presence or absence of tube hole serrations (grooves) (3) Tube hole size and tolerance (4) Tubesheet ligament width and its relation to tube diameter and thickness (5) Tube wall thickness (6) Tube hardness and change in hardness during cold working (7) Tube O.D. tolerance (8) Type of expander used (9) Type of torque control or final tube thickness control

(1 0) Function of tube joint, i.e. strength in resistance to pulling out, minimum cold work for corrosion purposes, freedom from leaks, ease of replacement, etc.

(1 1) Length of expanded joint (1 2) Compatibility of tube and tubesheet materials

RGP-RCB-7.6 TESTING OF WELDED TUBE JOINTS Tubetotubesheet welds are to be tested using the manufacturer’s standard method. Weld defects are to be repaired and tested. Any special testing such as with halogens, or helium, will be performed by agreement between manufacturer and purchaser.

RGP-RCB-9 CHANNELS, COVERS, AND BONNETS

RGP-RCB-9.21 FLAT CHANNEL COVER DEFLECTION The recommended limit for channel cover deflection is intended to prevent excessive leakage between the cover and the pass partition plate. Many factors govern the choice of design deflection limits. Some of these factors are: number of tube side passes; tube side pressure drop; size of exchanger; elastic springback of gasket material; effect of interpass leakage on thermal performance; presence or absence of gasket retaining grooves; and leakage characteristics of the tube side fluid. The method shown in Paragraph RCB-9.21 for calculating deflection does not consider: (1) The restraint offered by the portion of the cover outside the gasket load reaction diameter. (2) Additional restraint provided by some types of construction such as full face gasket controlled

metal-to-metal contact, etc. (3) Cover bow due to thermal gradient across the cover thickness.



The recommended cover deflection limits given in Paragraph RCB-9.21 may be modified if other calculation methods are used which accomodate the effect of reduced cover thickness on the exchanger performance. Reference: Singh, K.P. and Solar, A.I., "Mechanical Design of Heat Exchangers and Pressure Vessel Components", First Edition (1 984), Chapter 12, Arcturus Publishers, Inc.

RGP-RCB-10 NOZZLES

RGP-RCB-10.6 NOZZLE LOADINGS For purposes of desi n, nozzle loads are assumed to be negligible, unless the purchaser specifically

FIGURE RGP-RCB-10.6 details such loads in p1 is inquiry as indicated in Figure RGP-RCB-10.6.

Since piping loads can impose forces and moments in three geometric planes, there is no one set of values which can be provided as a maximum by the manufacturer. Each piping load should be evaluated as a combination of forces and moments as specified by the purchaser. Nozzle reactions from piping are transmitted to the pressure containment wall of the heat exchanger, and could result in an over-stressed condition in this area. The effects of piping loads transmitted through main body flanges, supports and other components should also be considered. For calculation of the combined stresses developed in the wall of the vessel due to piping and pressure loads, references are listed below. References: (1) Welding Research Council Bulletin No. 107, "Local Stresses in Spherical and Cylindrical Shells

(2) "Stresses From Radial Loads and External Moments in Cylindrical Pressure Vessels", P.P.

(3) "Local Stresses in Cylindrical Shells", Fred Forman, Pressure Vessel Handbook Publishing, Inc. (4) Pressure Vessel and Piping Design Collected Papers, (1927-1959), The American Society of

Mechanical Engineers, "Bending Moments and Leakage at Flanged Joints", Robert G. Blick. (5) ASME Boiler and Pressure Vessel Code, Section Ill, "Nuclear Power Plant Components". (6) Welding Research Council Bulletin No. 198, "Secondary Stress Indices for Integral Structural

(7) Welding Research Council Bulletin No. 297, "Local Stresses in Cylindrical Shells Due To External

Due to External Loading", K. R. Wickman, A.G. Hopper and J.L. Mershon.

Bijlaard, The Welding Journal Research Supplement (1954-1 955).

Attachments to Straight Pipe", W.G. Dodge.

Loadin s on Nozzles - Supplement to WRC Bulletin 107", J.L. Mershon, K.Mokhtarian, G.V. Ranjan and E. 8 . Rodabaugh.

RGP-RCB-11 END FLANGES AND BOLTING

RGP-RCB-11.5 LARGE DIAMETER LOW PRESSURE FLANGES When designing a large diameter, low pressure ffange, numerous considerations as described in Appendix S of the Code should be reviewed in order to reduce the amount of flange rotation. Another point of consideration is the fact that this type of flange usually has a large actual bolt area



compared to the minimum required area; the extra bolt area combined with the potential bolt stress can overload the flange such that excessive deflection and permanent set are produced. Methods are available to determine the initial bolt stress required in order to achieve a leak-free bolted joint. Once the required bolt stress is known, flange rotation and stress can then be calculated and, if necessary, the designer can take further action to reduce rotation and/or stresses.

RGP-RCB-11.6 BOLTING-ASSEMBLY AND MAINTENANCE The following references may be used for assembly and maintenance of bolted flanged joints. See Paragraphs E-3.24 and E-3.25. References: (1) Torque Manual. Sturtevant-Richmont Division of Ryeson Corp. (2) Crane Engineering Data, VC-l900B, Crane Company.

RGP-RCB-11.7 PASS PARTITION RIB AREA Gasket pass partition rib area contributes to the required bolt load, therefore, its effects should be considered in the design of flanges. One acceptable method to include rib area is shown below. Other methods are acceptable.

Y ’ = Y value of pass partition rib@)*

m’ = mfactor of pass partition rib(@*

b = Effective seating width of pass partition rib(s)*

r = Total length of pass partition rib@)*

W m, and W m2 = As defined in ASME Code

Pass Partition

Section VIII, Division 1 Appendix 2 and modified below.

W m 2 = b x G Y + b , r , Y ‘ Seating width of Partition Rib (N)

H , = Z P [ b n G m + b , r , r n ’ ]

H = ( G ) * ( P ) ( O . 7 8 5 4 )

W m , = H + H p

*Note:

(1) mand Yvalues for peripheral portion of gasket may be used if greater than m ’& Y ’

(2) n a n d Y values are listed in ASME Code Section VIll Div. 1, Appendix 2 Table 2-5.1 or as specified by gasket manufacturer.



RGP-T-2 FOULING

RGP-T-2.1 TYPES OF FOULING Currently five different types of fouling mechanisms are recognized. They are individually complex, often occurring simultaneously, and their effects may increase pressure drop, accelerate corrosion and decrease the overall heat transfer coefficient. (1) Precipitation Fouling

Crystallization is one of the most common types of preci itation fouling. It occurs in many process streams, cooling water and chemical streams. l rystallization scale forms as the result of over-saturation of a relatively insoluble salt. The most common, calcium carbonate, forms on heat transfer surfaces as a result of the thermal decomposition of the bicarbonate ion and the subsequent reaction with calcium ions.

Sedimentation is the most common form of particulate fouling. Particles of clay, sand, silt, rust, etc. are initially suspended in the fluid and form deposits on the heat transfer surfaces. Sedimentation is frequently superimposed on crystallization and possibly acts as a catalyst for certain types of chemical reaction fouling.

Surface temperatures and the presence of oxidation promoters are known to significantly influence the rate of build up of this fouling type. Coking, the hard crust deposit of hydrocarbons formed on high temperature surfaces, is a common form of this type of fouling.

Iron oxide, the most common form of corrosion product, is the result of an electro-chemical reaction and forms as a scale on iron-containing, exposed surfaces of the heat exchanger. This scale produces an added thermal resistance to the base metal of the heat transfer surface.

Organic material growth develops on heat transfer surfaces in contact with untreated water such as sea, river, or lake water. In most cases, it will be combined or superimposed on other types of fouling such as crystallization and sedimentation. Biological growth such as algae, fungi, slime, and corrosive bacteria represent a potentially detrimental form of fouling. Often these micro-organisms provide a sticky holding medium for other types of fouling which would otherwise not adhere to clean surfaces.

(2) Particulate Fouling

(3) Chemical Reaction Fouling

(4) Corrosion Fouling

(5) Biological Fouling

RGP-T-2.2 EFFECT OF FOULING There are different approaches to provide an allowance for anticipated fouling in the design of shell and tube heat exchangers. The net result is to provide added heat transfer surface area. This generally means that the exchanger is oversized for clean operation and barely adequate for conditions just before it should be cleaned. Although many heat exchangers operate for years without cleaning, it is more common that they must be cleaned periodically. Values of the fouling resistances to be specified are intended to reflect the values at the point in time just before the exchanger is to be cleaned. The major uncertainty is the assignment of realistic values of the fouling resistances. Further, these thermal resistances only address part of the impact of fouling as there is an increase in the hydraulic resistance as well; however, this is most often ignored. Fouling is complex, dynamic, and in time, degrades the performance of a heat exchanger. The use of thermal resistance permits the assignment of the majority of the fouling to the side where fouling predominates. It also permits examination of the relative thermal resistance introduced by the different terms in the overall heat transfer coefficient equation. These can signal, to the designer, where there are potential design changes to reduce the effect of fouling. It also permits the determination of the amount of heat transfer surface area that has been assigned for fouling. Higher fouling resistances are sometimes inappropriately specified to provide safety factors to account for uncertainties in the heat transfer calculation, the actual operating conditions, and/or possible plant expansion. These uncertainties may well exist and should be reflected in the design, but they should not be masked in the fouling resistances. They should be clearly identified as appropriate factors in the design calculations.



Another inappropriate approach to heat exchanger design is to arbitrarily increase the heat transfer surface area to allow for fouling. This over-surfacing avoids the use of the appropriate fouling resistances. In effect, the fouling for the exchanger is combined and no longer can be identified as belonging to one side or the other. In order to examine the effect of fouling on the pressure drop, it is necessary for the purchaser to supply the anticipated thicknesses of each of the fouling layers.

RGP-T-2.31 PHYSICAL CONSIDERATIONS A) Properties Of Fluids And Usual Propensity For Fouling

The most important consideration is the fluid and the conditions when it produces fouling. At times, a process modification can result in conditions that are less likely to cause fouling.

For many kinds of fouling, as the temperatures increase, the amount of fouling increases. Lower temperatures produce slower fouling build-up and deposits that often are easier to remove.

Normally, keeping the velocities high reduces the tendency to foul. Velocities on the tube side are limited by erosion, and on the shell side by flow-induced vibration. Stagnant and recirculation regions on the shell side lead to heavy fouling.

The selection of tube material is significant when it comes to corrosion. Some kinds of biological fouling can be lessened by copper-bearing tube materials. There can be differences between finned and plain tubing. Surface finish has been shown to influence the rate of fouling and the ease of cleaning.

The geometry of a particular heat exchanger can influence the uniformity of the flows on the tube side and the shell side. The ease of cleaning can be greatly influenced by the orientation of the heat exchanger.

The fouling resistances for the same fluid can be considerably different depending upon whether heat is being transferred through sensible heating or cooling, boiling, or condensing.

Most fluids are prone to have inherent impurities that can deposit out as a fouling layer, or act as catalysts to the fouling processes. It is often economically attractive to eliminate the fouling constituents by filters.

H) Fluid Treatment To Prevent Corrosion And Biological Growth Fluid treatment is commonly carried out to prevent corrosion and/or biological growth. If these treatments are neglected, rapid fouling can occur.

There are additives that can disperse the fouling material so it does not deposit. Additives may also alter the structure of the fouling layers that deposit so that they are easily removed. The use of these treatments is a product quality and economic decision.

One of the effective ways to reduce the possibility of corrosion and corrosion fouling is to provide cathodic protection in the design.

B) Surface And Bulk Temperatures

C) Local Velocities

D) Tube Material, Configuration And Surface Finish

E) Heat Exchanger Geometry And Orientation

F) Heat Transfer Process

G) Fluid Purity And Freedom From Contamination

I ) Fluid Treatment To Reduce Fouling

J) Cathodic Protection



K) Planned Cleaning Method And Desired Frequency It is important that the cleaning method be planned at the design stage of the heat exchanger. Considerations in design involving cleaning are whether it will be done on-line, off-line, bundle removed or in place, whether it will involve corrosive fluids, etc.. Access, clearances, valving, and piping also must be considered to permit ease of cleaning. The cleaning method may require special safety requirements, which should be incorporated in the design.

There are two benefits from placing the more fouling fluid on the tube side. There is less danger of low velocity or stagnant flow regions on the tube side, and, it is generally easier to clean the tube side than the shell side. It is often possible to clean the tube side with the exchanger in place while it may be necessary to remove the bundle to clean the shell side.

L) Place The More Fouling Fluid On The Tube Side

RGP-T-2.32 ECONOMIC CONSIDERATIONS Planned fouling prevention, maintenance and cleaning make possible lower allowances for fouling, but do involve a commitment to ongoing costs. The amount and frequency of cleaning varies considerably with user and operation. The most si nificant that should % 8 " e provi ed are the operational and economic factors that change with time. New fluid treatments, changing first costs and operating costs, different cleaning procedures and the degree of payback for longer periods of being on stream should be some of the items evaluated in determining an appropriate fouling resistance. Failure to include the economic considerations may lead to unnecessary monetary penalties for fouling. Companies concerned about fouling continually monitor the performance of their heat exchangers to establish fouling experience and develop their own guidelines for determining the appropriate fouling resistance to specify when purchasing new equipment. Almost every source of cooling water needs to be treated before it is used for heat exchanger service. The treatment ranges from simple biocide addition to control biological fouling, to substantial treatment of brackish water to render it suitable for use. The amount of treatment may be uneconomical and substitute sources of cooling must be sought. With today's technology, the quality of water can be improved to the point that fouling should be under control as long as flow velocities are maintained and surface temperatures controlled.

rameters involved in deciding upon the amount of fouling allowance

RGP-T-2.4 DESIGN FOULING RESISTANCES (HR FT* O F/Btu) The purchaser should attempt to select an optimal fouling resistance that will result in a minimum sum of fixed, shutdown and cleaning costs. The following tabulated values of fouling resistances allow for oversizing the heat exchanger so that it will meet performance requirements with reasonable intervals between shutdowns and cleaning. These values do not recognize the time related behavior of fouling with regard to specific design and operational characteristics of particular heat exchangers.


SECTION 10

Fuel Oil #2 Fuel Oil #6

Transformer Oil Engine Lube Oil Quench Oil


0.002 0.005 0.001 0.001

0.004

Exhaust Steam (Oil Bearing) Refriaerant Vaoors (Oil Bearing)

I Enaine Exhaust Gas Io.010 I

0.001 5-0.002 0.002

1 - ~~ ~~~

Steam (Non-Oil Bearing) 10.0005 1

Compressed Air Ammonia Vapor

0.001

0.001

Coal Flue Gas Natural Gas Flue Gas

I CO Vapor Io.001 I 0.01 0 0.005

I Chlorine Vapor 10.002 I

Refrigerant Liquids Hydraulic Fluid Industrial Organic Heat Transfer Media

0.001 0.001

0.002 Ammonia Liquid Ammonia Liquid (Oil Bearing) Calcium Chloride Solutions Sodium Chloride Solutions

0.001 0.003 0.003 0.003

CO Liquid

~

Methanol Solutions Ethanol Solutions

Io.001

0.002 0.002

I Chlorine Liauid 10.002 I

I Ethvlene Glvcol Solutions 10.002 I



Acid Gases Solvent VaDors

SECTION 10

0.002-0.003 0.001

Fouling Resistances For Chemical Processing Streams Gases And Vapors: 1

MEA And DEA Solutions DEG And TEG Solutions

0.002 0.002

Caustic Solutions Vegetable Oils

I Stable Side Draw And Bottom Product I 0.001 -0.002 I 0.002 0.003

' Gases And Vapors: >

Natural Gas 0.001 -0.002 Overhead Products 0.001 -0.002

'

I Natural Gasoline And Liquified Petroleum Gases I 0.001 -0.002 I

Liquids:

Lean Oil 0.002 Rich Oil 0.001 -0.002


SECTION 10

Atmospheric Tower Overhead Vapors Light Naphthas Vacuum Overhead Vapors


0.001 0.001 0.002

0 to 250 O F VELOCITY K/SEC

<2 2-4 >4

DRY 0.003 0.002 0.002 SALT* 0.003 0.002 0.002

350 to 450 O F VELOCITY FT/SEC

<2 2-4 >4

DRY 0.004 0.003 0.003 SALT* 0.006 0.005 0.005

*Assumes desalting @ approx. 250 O F Gasoline 10.002

250 to 350 O F VELOCITY IT/SEC

<2 2-4 >4

0.003 0.002 0.002 0.005 0.004 0.004

450 O F and over VELOCITY K/SEC

<2 2-4 >4

0.005 0.004 0.004 0.007 0.006 0.006

288

Naphtha And Light Distillates Kerosene Light Gas Oil Heavy Gas Oil Heavy Fuel Oils

0.002-0.003 0.002-0.003 0.002-0.003 0.003-0.005 0.005-0.007


Vacuum Tower Bottoms Atmosphere Tower Bottoms

0.010

0.007

Overhead Vapors Light Cycle Oil Heavy Cycle Oil Light Coker Gas Oil Heavy Coker Gas Oil Bottoms Slurry Oil (4.5 Ft/Sec Minimum) Light Liquid Products

0.002 0.002-0.003 0.003-0.004 0.003-0.004 0.004-0.005 0.003 0.002


Hydrocracker Charge And Effluent* Recycle Gas Hydrodesulfurization Charge And Effluent* Overhead Vapors

SECTION 10

0.002 0.001

0.002

0.001

Fouling Resistances For Oil Refinery Streams- continued Catalytic Reforming, Hydrocracking And Hydrodesulfurization Streams:

Reformer Charge I 0.001 5

Liquid Product 30 - 50 O A.P.I.

I Reformer Effluent I 0.001 5 I

0.002

Overhead Vapors And Gases Liquid Products Absorption Oils

~~~

Liauid Product Over 50 O A.P.I.

0.001

0.001

0.002-0.003

10.001

Solvent Feed Mix Solvent Extract* Raff inate

0.002 0.001

0.003 0.001

~

Asphalt Wax Slurries* Refined Lube Oil

I Alkviation Trace Acid Streams 10.002 I

0.005

0.003 0.001

I -

I0.002-0.003 ~

Reboiler Streams I

Overhead Vapor Visbreaker Bottoms

Lube Oil Processing Streams: Feed Stock 10.002

0.003 0.01 0

Effiuent Naohthas

0.002 0.002

I *Precautions must be taken to prevent wax deDosition on cold tube walls. I

I Feed 10.003

I Overhead Vapors I0.0015 I


SECTION 10

Charge Effluent H.T. Sep. Overhead Strimer Charqe


0.004-0.005

0.002 0.002

0.003

Fouling Resistances for Oil Refinery Streams - continued

Alkylate, Deprop. Bottoms, Main Fract. Overhead Main Fract. Feed

Catalytic Hydro Desulfurizer: I

0.003

Temperature Of Heatina Medium Temperature Of Water

UD To 240" F 240 to 400" F 125 OF Over 125" F

I All Other Process Streams 10.002 I

Sea Water 0.0005 0.0005 0.001 0.001 Brackish Water 0.002 0.001 0.003 0.002

Cooling Tower And Artificial Spray Pond:

Treated Make Up 0.001 Io.001 10.002 10.002

Fouling Resistances For Water

city Or Well Water River Water:

Minimum

0.001 Io.001 0.002 10.002

0.002 Io.001 10.003 10.002

I I Water Velocity Ft/Sec I Water Velocity Ft/Sec I

Average Muddy Or Silty Hard (Over 15 Grains/Gal.) Engine Jacket

~~ ~~ ~~ 1 3 and Less 1 Over 3 13 and Less I Over 3 1

0.003 0.002 0.004 0.003

0.003 0.002 0.004 0.003

0.003 0.003 0.005 0.005

0.001 0.001 0.001 0.001

Treated Boiler Feedwater Boiler Blowdown

0.001 0.0005 0.001 0.001

0.002 0.002 0.002 0.002

I Distilled Or Closed Cvcle I I -

Condensate 0.0005 I0.0005 I0.0005 10.0005 1

If the heating medium temperature is over 400 O F and the cooling medium is known to scale, these ratings should be modified accordingly.


INDE

A

Acoustic Resonance or Coupling .......................................... 95 . 117 Air Test ........................................................................................... 24 Allowable Working Pressure of Tubes ....................... 233, 234, 235 Alloy, TEMA Definition ......................................... Alloy Clad Tubesheets Alloy Shells, Minimum Anodes ........................ Area,

Bundle Entrance and Exit ........................................ 35, 274-278 .... 248

ASME Code Data Reports ............................................................ 14 Segments of Circles ...................................

B

B Class Heat Exchanger. Definition ............................................. 23

Baffles and Support Plates , ........................................................... 31 Cross, Clearances ............................................................. 31, 32 Cross, Minimum Thickness ............................................... 32, 33 Cuts ............................................. Holes .................................................................... Impingement ............................................................................ 35 Longitudinal ................................. Spacing ........................................ Special Cases .......................................................................... 34 Special Precautions .............................................. Type .............................................

Backing Devices ..................................................................... 38, 39

Bolted Joints .................................................................................. 19 Bolting,

Dimensional Data ................................. End Flanges .......................................... Foundation ......................................... Internal Floating Head ....................... Pass Rib Area .................................... Size and Spacing ..................................................................... 93 Tightening ............................................................................... 19 Type ..................................................................................... 94

Bundle Cleaning .................................................................... 21, 22 Bundle Entrance and Exit Area ..................................................... 35 Bundle Hold Down ................................................................... 36, 37 By-Pass Valves ....................................

c

C Class Heat Exchanger. Definition .............................................. 23 Cast Iron. Service Limitation ......................................................... 25 Channel Covers ............................................................ 88, 280, 281 Channel Cover Formula ................................. Channel Cover Grooves ................................. Channel Pass Partitions .......................................................... 88 . 89 Channels, Minimum Thickness ........ ............... 88 Channels. Type Designation & Size ........................ 1. 2 Circular Rings and Discs,

Weights of ......................................... Circular Segments. Areas of .................. Cleaning Heat Exchangers ................................................ 18. 21. 22 Cleanliness. Inspection .................................. Cleanliness Provisions .................................. Clearance, Cross Baffles & Support Plates .................................. 32 Clearance. Wrench & Nut .................................................... 188, 189 Code Data Reports ....................................................................... 14 Compressibility Charts. Generalized Gas .................. 156. 157. 158 Compressibility. Gas ............... ........................................

Connections. Pressure Gage ........................................................................ 91 Protection ................................................................................ 17 Stacked Units ..................................................................... 91 . 92

Construction Codes

Correction Factors for Mean Temperature Difference ....................................................................... 134-146

Correction Factors for Bolting Moment ......................................... 93 Corrosion and Vibration ................................................................. 14 Corrosion Allowance ................................................................ 24, 25 Counterflow Exchangers ............................................ 127, 133, 147 Covers,

............................................... 88 . 280, 281

................................................................ 31 Critical Properties ................................................................ 152 . 182 Cross Baffles ............................................ ........................... 31-34

Floating Head ....................................................

Damages. Consequential .............................................................. 14 Data Reports .................................................... Defective Parts ........................

.............................. 10 Density.

Gases ............................................................ 150. 156. 157. 158 tiauids ................................................................... 150. 154. 155

Design Conditions .......................................................................... 18

Design Temperatures ........................................................ 24 Diameters.

Baffle and Support Plate. Tube Holes .................................... 31 Tubesheet Holes .... ..................................................... 7 0 ~ 71

Design Pressures ........................ .................................. 23

Dimensions. Bolting ............................................................................ 188. 189 Fittings. Welding .................................................................... 185

..................................................................... 230~ 231

Flanges, ASME .......................................... Pipe, Welded and Seamless .....................

Dirt ................................................... Disassembly for Inspection ............................ Dismantling Clearance .................................................................. 17 Double Tubesheets ................................................................... 55-62 Drain Connections ................. .......................... 18. 56. 91 Draining Exchangers ............. 18. 20 Drawings .................................................................................. 13. 14 Drift Tolerance. Tube Hole Drill ............................................... 72. 73 Drilling Tolerance. Tubesheets ........................

................................

E

Elasticity. Modulus of ......... ............................................. 236. 237 .......................... 25. 93. 94, 281. 282

Entrance ti Exit Areas. Tube Bundles ........................... 35, 274-278 Exchangers (See Heat Exchanger) Expansion Joints. Shell ................................... Expansion, Mean Coefficients of Thermal ......

End Flanges .......................

Expanded Tube Joints .................. 22, 72. 73, 280 ...........

Standards of the Tubular Exchanger Manufacturers Association 291

Fabrication Inspection .................................................................. 13 Fabrication Tolerances ................................................................. 6-9 Facilities for Cleaning Heat Exchangers ................................. 21, 22 Finish, Tube Holes ................................................................. 70. 280 Fittings, Dimensions of Welding .................................................. 185 Fixed Tubesheets ..................................................... 46, 53, 62-70 Flanges,

End .................................................... 25, 93, 94, 281, 282 ASME Standard. ............................................... 186, 187 Bolt Clearances ....................................................... 188, 189 Split Type ................................................................................. 92 Pressure-Temperature Rating ...................................... 190-229 Protection ................................................................................. 15

Flexible Shell Elements ............................................................ 75-88 Floating Heads ,.............. ................................................................ 38

Backing Devices ................................................................ 38, 39 Packed ......................................................................... 40, 41, 42 Internal ......................................................................... 38, 39 . 40 Nomenclature ............................................................................ 3 Outside Packed ........................................................... 40, 41, 42 Packed Lantern Ring ............................................................... 42 Tube Bundle Supports ............................................................. 40

Floating Tubesheet .......................................

Fluid Temperature Relations ........................ Fouling,

Fluid Density .................................................

Economics of ................................................................. 126, 285 Effect of ................................................................ 126, 283 . 284 Indication of ............................................................................ 19

Chemical Processing Streams ........................................... 287 Industrial Fluids ..................................................................... 286 Natural Gas-Gasoline Processing Streams .......................... 287

....................... 288, 289 . 290 Water ......................

Fouling Resistance.

Oil Refinery Stream

Foundation Bolts ..................................................... Foundations .........................................

Gages. Standard Diameters ............................................... Gaskets (Peripheral 8 Pass Partition) ....................

Material .................................................................................... Replacement ...................................................... Joint Details ....................................................................... 43. 44

General Construction Features ............................................... 15, 16 Generalized Compressibility Charts ........................... 156, 157, 158 Grooved Channel Covers .............................................................. 90 Grooved Tube Holes .................................................... Grooved Tubesheets .................................................... Guarantees .............................................................................. 14, 15

H

Handling Tube Bundles ................................................................. 21 Hardness Conversion Table ........................................................ 232 Heat Content Petroleum Fractions ...................................... 151 . 167 Heat Exchanger Arrangement Diagrams, ..................... ..... 2-5

Parts and Nomenclature .......................... ............... 3, 4, 5 Standard Dimension Tolerance ............................................. ~9

Holes, .......... ......................................................................... 70

Diameter and Tolerance, Tube .................................... 70, 71 Finish, Tube .................................................................... 70, 280 Grooving .......................................................................... 71

Hydrostatic Test Pressure ............................................................ 23

Baffles and Support Plates .............................................. 31, 122

I

Impingement Baffles. Bundle Entrance and Exit Areas ............................................. 35 Protection Requirements ......................................................... 35 Shell and Tube Side ................................................................ 35

Inspection, Cleanliness ............................................................ 15 . 19 Inspection, Fabrication .................................................................. 13 Installation of Heat Exchangers ............................ Internal Floating Heads .......................

J

Jacketed Gaskets .......................................................................... 43 Joints,

Bolted ...................................................................................... 19 Packed. Service Limitations ........................................ 40. 41. 42

K

Kettle Type Reboiler. Typical Illustration .................................... 2 ,5

L

Latent Heats of Various Liquids ...................................

Leveling H Lifting Dev .....................................

Load Concentration Factor, Flanges ............ Longitudinal Baffles ......................................

Leaks, Locating ........................................................................ 20. 21

Ligaments ets Minimum ................

gers ............................................................ 17

Maintenance of Heat Exchangers ............................................ 19-22 Material Warranties ..................................................... Materials- Definition of Terms ..................... ............................. 23 Mean Coefficients of Thermal Expansion ........................... 238, 239 Mean Metal Temperature ..................................... 24, 128, 129, 130 Mean Temperature D

(See also MTD) Metal Resistance, Finned & Bare Tubing ................................... 125 Metal Temperature Li Minimum Inside Dept Minimum Inside Depth Floating Heads ................ Modulus of Elasticity .......... MTD Correction Factors ....

292 Standards of the Tubular Exchanger Manufacturers Association

N

INDEX

S

Name Plates ................................................................................ 13 Natural Frequencies, Tubes .......................................................... 97 Nomenclature of Heat Exchanger Components ............................. 3 Nomenclature ................................................................................ 1-5 Nozzles,

Connections ....................................................................... Floating Head .......................................................................... 40 Loadings .......................................................................... 92, 281 Split Flanges ............................................................................ 92

Number and Size of Tie Rods ................................................. 35, 36

0

Operation of Heat Exchangers ................................................ 18, 19 Operating Procedures ............................................................. 18, 19 Outside Packed Floating Head ......................................... 40, 41, 42

P

Packed Floating Heads ..................................................... 40, 41, 42 Packing Boxes ................................................................... 26, 40, 41 Packing Material ............................................................................ 42 Parts, Replacement ................................................................. 15, 22 Pass Partition Grooves ............................................................ 74, 90 Pass Partition Plates ............................................................... 88, 89 Pass Partition Rib Area ............................................................... 282 Performance Failures .................................................................... 17 Performance Guarantees .............................................................. 14 Periodic Inspection .................................................................. 19, 20 Physical Properties of Fluids ..................................... Pipe .

Dimensions of Welded and Seamless .................................. 184 Shells ...................................................

......................................................... 91

................................................. 92, 281 Pipe Tap Connections ....

Pitch, Tubes ...................................................... Plate, Shells ...................................................... Plugging Tubes in Tube Bundles .......................................... 22 . 273 Postweld Heat Treatment,

Floating Head Covers .............................................................. 38 Channels and Bonnets ............................................................ 89

Preparation of Heat Exchanger for Shipment ............................... 15 Pressure Gage Connection ........................................................... 91 Pressure Loss .............................................................................. 126 Pressure-Temperature Ratings for Valves, Fittings,

and Flanges ................................................................... 190-229 Pressure, Tube Working ...................................................... 232-235 Protection,

Piping Loads ...................

Impingement ................................................... Shipment ............................

Pulling Mechanisms ....................................... Pulsating Fluids .............................................

R

R Class Heat Exchanger. Definition .............................................. 23 Ratings. Valves. Fittings. and Flanges

Reboiler. Kettle Type. Illustration .................................................... 5 Recommended Good Practice. RGP Section ............................. 252 Replacement Parts ........................................................................ 15 Removing Tube Bundles .............................................................. 21 Ring Flanges. Split ........................................................................ 92 Rings. Weights of ............................................................ 242-247

[See Pressure-Temperature Ratings)

Safety Relief Devices ................................................................ 18 Sealing Devices ........................................................................... 36 Seamless Pipe, Dimensions of ..... ...................................... 184

.................................................. 248

.................................... 16, 253-268

Longitudinal Stress . Minimum Thickness ................................................................. 30 Size Numbering &Type Designation .................................... 1 ,2

Shop Operation .............................................................................. 13 Shutting Down Operation .............................................................. 18 Size Numbering of Heat Exchangers .............................................. 1

Specific Gravity ,.. ......................................................................... 150 Hydrocarbon Liquids ..........................................

Gases, Miscellaneous, Atmospheric Pressure ..................... 165 Gases at High Pressure ....................................... 150, 151, 166

Atmospheric Pressure ............................ 150, 161, 162, 163

Petroleum Fractions, Liquid ......................................... .150, 159 Petroleum Fractions, Vapor .......................................... 150, 160

Tolerances ................. ....................................................... 30 s ..................................................... 15 Shipment, Preparation of

Spacers and Tie Rods ..................... Spare Parts ...................................... ...................... 15, 22, 44

Specific Heat ,... ..................... .......................................... 150 . 151

Hydrocarbon Gases,

Liquids, Miscellaneous ............................................. 150, 164

Specification Sheet, Split Type Nozzle FI Stacked Units .......... Starting Operation ...................... Stress Relieving (See Postweld Heat Treatment) Support Plates,

.............................................. 1 1, 12

.................................................... 31

..................................... 33, 34, 121

.............................................. 32, 33

...................... 6, 7, 15, 16, 253-268

T

Temperature. ................................................................ 24 .............................................................. 127

Shocks .............................................. .................................. 19 .......................... 27. 128 Temperature Efficiency, ..........................

Counterflow Exchangers ....................................................... 147 1 Shell Pass ........................... 2 Shell Passes .........

Test Connections ........... Test, Pneumatic or Liqui

Test Ring ........................ Thermal Conductivity, ....

Conversion Factors . Gases and Vapors, Miscellaneous ....................................... 172 Liquids, Miscellaneous .......................... Liquid Petroleum Fractions ........................... Metals ............................................................................. 240, 241 Pressure Correction . ...................................... 173. 174 Pure Hydrocarbon Liquids ..................................................... 170

Thermal Expansion, Mean Coefficients of, Metals ....... Thermal Performance Tes Thermal Resistance of Un Thermal Relations ........................................................................ 124 Thermometer Connections ........

Standards of the Tubular Exchanger Manufacturers Association 293

Thickness. Minimum. Baffles ......................................................................... 32, 33 Channels and Bonnets ............................................................ 88 Channel Covers ...................................................... 90, 280, 281 Shells and Shell Covers ................................................... 30. 31 Tubes .............................................................................. 27, 28 Tubesheets .............................................................................. 45

Tie Rods and Spacers, Number and Size ............. Tolerances,

Tube Holes in Tubesheets ............................... Tube Holes in Baffles ...........................

Shells and Shell Covers ........................................... . 30 Tubesheet Drilling .............................................................. 70. 71

Cleaning . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 18, 21, 22 Handling . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 21 Plugging Tubes ............................................................ 22, 273 Removal ..........................................................................

............................................................... 14

Heat Exchangers and Parts ................................................... 6-9

Tube Bundles,

....................................................................

.................................................................... Tube Joints,

Expanded ............................................................ 22, 72, 73, 280 Loads ................................................................................. 69, 70 Testing, Welded ..................................................... Welded ...................................................................

(See Also Support Plates) Tube Support Plate Drilling ........................................................... 31

Tube Wall Metal Resistance ................. ................................. 125

Tubes, Tube Working Pressure, Internal ......... ................ 233, 234, 235

Characteristics .............................. ............................ 230, 231 Compressive Stress ................................................................ 69 Diameters and Gages ............................................................. 27 Expanding ................................................................................ 22 Finned ...................................................................................... 27 Leaks ................................................................................. 20, 21 Length ...................................................................................... 27 Longitudinal Stress ............................................................ 67, 68 Maximum Recommended Gages .......................... Natural Frequencies ...............................................

...................................................................... 28, 29

............................................................................ 29 ube Bundles ..................................................... 273

Projection ................................................................. Special Precautions ................................................. Tube Wall Reduction ............................................... U-Tubes .................................................................... 28, 96, 104 Unsupported Length, Maximum ....... Working Pressure, Internal ...............

Application Instructions & Limitation Applied Facings ....................................................................... 45 Clad & Faced Tubesheets ............................................. Divided Floating Heads ........................................................... 46 Double Tubesheets ............................................................ 55-62 Effective Tubesheet Thickness ............................................... 45 Fixed Tubesheets .................................................. 46, 53, 62-70 Fixed Tubesheets of Differing Thickness ......................... 66, 67 For mu lae ,

Bending ....................................................................... .4 6-49 Effective Design Pressures-Floating Head (Type P) ....... 55 Effective Differential Design Pressure ....................... 65, 66 Effective Shell Side Design Pressure ........................ 64, 65 Effective Tube Side Design Pressure ............................... 65 Equivalent Bolting Pressure ........................................ 63, 64

Tubesheets. ...............................................................

Tubesheets. Formulae. (continued) Equivalent Differential Expansion Pressure ............... 62. 63 Flanged Extension ...................................................... 53. 54 Shear ..................................................................... 5 0 ~ 51. 52 Shell Longitudinal Stress ................................... 67. 68, 279 Tube Allowable Compressive Stress ................................ 69 Tube Longitudinal Stress ...... ....................... 68. 69 . 279

................................. 69. 70 I ntegr a1 I y .................................................................. 45 Minimum s .............................. ............................. 45 Packed Floating Tubesheet Type

................................................ 40~ 41. 42

Tubsto-Tubesheet Joint Loa

dinal Stresses ........................ 67. 68 . 69 Special Cases .......................................................................... 70 Tube Holes in Tubesheets ................................................ 70. 71 Tube Joints-Expanded & Welded ............................ 22. 74 . 280 Tubesheet Pass Partition Grooves ....................................... 74 Tubesheet Pulling Eyes .................................................. 74

Type Designation of Heat Exchangers ...................................... 1 . 2

U

Unsupported Tube Length. Maximum ..................................... 33, 34 .................................................................. 28 .................................................................. 34

Heat Treatment ........................................................................ 28 Users Note .................. ................................................ VIII

v

Vent & Drain Connections ................................................. 18, 56, 91 Vibration, ........................ ...................... 14, 34 . 35, 95-123

Acoustic Resonance ng .................................... 95, 1 16 Mechanisms Causing ............................................................. 95 Designs & Considerations ............................................. 121, 122 Selected References ..................................................... 122, 123 Tube Excitation ............................................................ 97, 98 . 99 Tube Natural Frequencies ..... Turbulent Buffeting ................ ............................. 116, 117 Vortex Shedding ........................................................ 116

Viscosity, ..................................................... 151 Conversion Factors ...................................... 151, 175, 249, 250 Gases & Vapors, Atmospheric Pressure .............................. 181 Gases & Vapors, High Pressure ................................... 151, 182 Hydrocarbons & Petroleum Fractions ........................... 176-179 Liquids, Miscellaneous .......................................................... 180

Wall Resistance. Finned & Bare Tubes ...................................... 125 Water Fouling Resistances ......................................................... 290 Weights of Circular Rings & Discs ... Weights of Tubing ............................. Welded and Seamless Pipe. Dimensions of ............................... 184 Welded Tube Joints ................................. 74. 280

294 Standards of the Tubular Exchanger Manufacturers Association

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TEMA_EighthEdition