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SOLDIER CREEK ENGINEERING
t TECHNICAL SERVICES, LLC Calculation SCE-FRNP-2019-M001
Rev. 0
Originated By: K.L. Kaylor
Checked By: T. Fletcher
Soldier Creek Engineering & Technical Services Document No.
SCE-FRNP-2019-M001 Page 1 of 19
Title: Nitrogen Piping Project Pressure Loss-Longest Run FRNP ESQ: FA5270
Responsible Engineer: K.L. Kaylor, P.E.
Date: 03/07/2019 Checked By: Terry Fletcher/ P.E.
Contents of Calculation _Page Number1.0 Summary 1
2.0 Detailed Problem Statement 1
3.0 Assumptions 1
4.0 References 1
5.0 Design Inputs 1
6.0 Analysis 2
7.0 Conclusions 2
Attachments 3
1.0 Summary
This calculation will determine the pressure drop of the longest run of the 6-in natural gas
supply header, from the tie-in to the 6-in natural gas supply at the package boiler area, to the 2-
in feed to C-300 for supply of natural gas for the HVAC Service Replacement project.
2.0 Detailed Problem Statement
This calculation is the first step in determining the expected pressure at each of the new header
takeoff feeds for suppling natural gas for the HVAC Replacement Service projects at C-100/ C-
200, and C-300. It is expected that the pressure drop from the supply to the feeds is small. Thus
the first calculation is for the longest run using conservative inputs (using total flow rate from
start to end, and a conservative length of pipe). If the calculated pressure drop is negligible/
then the pressure at each take-offfeed will be considered to be the same as the starting supply
pressure and calculating the pressure drop for each section of the header will not be required.
3.0 Assumptions
See Attachment 1. All assumptions are noted in the various sections of the calculation.
4.0 References
See Attachment 1. References are noted in the attachment.
5.0 Design Inputs
See Attachment 1. All inputs are noted in the various sections of the calculation.
Page 1 of 19
SOlDB)Cfi££KE»GW££R)NG
irecHWALSCTviusLic Calculation SCE-FRNP-2019-M001
Rev. 0
Originated By: K.L. Kaylor
Checked By: T. Fletcher
6.0 Analysis
See Attachment 1 for calculation details.
7.0 Conclusions
The calculated pressure drop of the longest run, supply tie-in connection to the 2-in feed to C-
300, is negligible, less than 0.04 psi. Thus the pressure at C-100 and C200 supply take-off feeds
will be considered to be the same as the starting supply pressure.
Responsible Engineer ^. L /^^u^ 03/07/19
Checker _\CU^^--- 2\?r\\^
Approverrtl^/^&U^ 3/^7, (9
Page 2 of 19
Calculation: SCE-FRNP-2019-M001 Rev. 0
Attachment 1
Calculation-NG Supply-Pressure Drop 1-Longest Run (2019-0213) 5 - pagesAttachment A - Calculation References 11 - pages
Page 3 of 19
Natural Gas Supply-Pipe Pressure Drop Calculation 1-Longest Run02/13/19 By: KL Kaylor
Using Crane example calculation 7-10
Crane Flow of Fluids-Technical Paper 410 - 2018 pg 7-6
Inputs
Outputs
Calculate pressure drop:
Longest Run-total flow from package boiler NG tie-in to C300 2-in supply takeoff from 6-in nitrogen piping header
Refl 6-4 Eqn6-22
Using: Darcy Weisbach equation - pressure drop in units of pounds per square inch (psi)
2.799xlQ~7KW2VAP=
d4
where:
K= resistance coefficient (unitless)
W= rate of flow (pph)
V= specific volume of fluid (cuft/lb)
d= internal diameter (in)
psi (Pressure loss)
Ref3.1
Assume:
Ref3.3
Ref3.2
Ref3.2
Ref3.2
Ref5
Given:
Fluid: Natural Gas
Sect 1.0 pl=
Pl=
Note 3 t=
Sg=
NG flow rate=
NG flow rate=
NG flow rate=
60 psig14.7 psia
74.7 psia
70 °F
0.59
99.0 cfm
37.1 cfm
12.4 cfm
Calculate total natural gas flow rate in pph:
Printouts
W,ioo=
wc-200=
W,300=
0.051 Ibs/cuft
302.9 pph
113.5 pph
37.9 pph
pressure (Ranges from 58-67)
barometric pressure
pressure
temperature
specific gravityC-100
C-200
C-300
density Note 6
C-100 flow rate
C-200 flow rate
C-300 flow rate
\N= 454.3 pph
Given: Pipe DetailsNom Size= 6 in
Material ASS CS
Sch= 40
Refl 6-2 Eqn6-3
Calculate reynolds number
6.3151^Re =
d[i
Refl
Refl
Refl
where:
W= rate of flow (pph)
d= internal diameter (in)
\i= absolute viscosity (centipoise)
B-14 d= 6.065 in
A-6 |j= 0.0106 centipoise
(linear interpolation & Note 2 )
solving:
A-26
Re= 4.46E+04
f= 0.0225
flow total
pipe size
pipe typepipe schedule
Reynolds number (unitless)
pipe IDabsolute viscosity
@ 74.7 psia70 OF
0.59 Sg hydrocarbon vapor
Reynolds number
friction factor (from Moody Chart)
Calculation-NG Supply-Pressure Drop 1-Longest Run (2019-0213) Page 4 of 19
Ref5 Printoutl
Refl
Refl
1-8
6-2 Eqn6-2
Calculate total resistance coefficient K
From Worksheet "K Calcs" below - Sum all K values for pipe, valves, and fittings
K= 154.00 resistance coefficient (total)
V= 3.902 cuft/lb specific volume
@ 60 psig70 OF
Calculate pressure loss
AP=| 0.03]psi Pressure loss
pressurep2=
% Change
59.97 psig
0.0% ( If ~ 10% less than inlet absolute pressure Pl, "OK", see Note 1)
(If not- see Refl pg 1-8 for correction directions)
Calculate velocity and compare to recommended
0.050931^v =
pd2 ft/s (Velocity)
where:
W= rate of flow (pph)p= density of fluid (Ib/cuft)
d= internal diameter (in)
Ref2
from above:
from above:
solving:
w=d=
p=
v=
v=\
454.3 pph6.065 in
1/specific volume (\3.902 cuft/lb
2.45|ft/s
Recommended velocity in pipes
100 ft/s
specific volume
velocity
Natural gas
References
Refl
Ref2
Crane Flow of Fluids-Technical Paper 410 - 2018
Internet-EngineeringToolbox-Liquids, gases and vapors - suggested fluid velocities in pipes
http://www.engineeringtoolbox.com/fluid-velocities-pipes-d_1885.html
RefS.l Project SOW
Ref3.2 NG Consumption (Handout at 12/20/18 meeting-draft)
Ref3.3 ATMOS ENERGY Gas Chemistry Report dated 12/11/18
Ref4 Sketch (20181221KLK)
Ref5 Internet-GlobalSpec-Gas Density and Specific Volume Calculator
http://www.globalspec.com/calculators/gas-density
Ref6 Reducer dimension chart
Ref7 Cameron Hydraulic Data - 16th Addition, 2nd Printing 1981
Notes:
1 From Refl page 1-8.
If the calculated pressure drop (AP ) is ~ 10% less than inlet absolute pressure Pl,
reasonable accuracy will be obtained if the specific volume (V) used in the
equation is based upon either the upstream or downstream conditions.
2 Graph values are gases at 14.7 psia; it's note states that for gas on this page, correction of viscosity for
pressure is <10% for pressures up to 500 psia; therefore assumed no correction in this calculation.
3 Assume 70F for convenience for initial calculation; gas source is underground at ~50F,
4 In K Calcs below, for convenience, used L/D's from Cameron Hydraulics Ref7. Crane 2018 is fairly
complicated and with negligible pressure drop, not worth all the calculations described in
pages 2-14 thru 2-16 as referred in A-30 for standard tees and wyes.
5 Not used.
6 Density at 14.73 psia (0 psig) and 60F, conditions used to estimate volumetric flow rate provided in reference 3.2.
Calculation-NG Supply-Pressure Drop 1-Longest Run (2019-0213) Page 5 of 19
Worksheet
Refl
"K Calcs"
Calculate resistance coefficient (K) values for pipe, valves,
From above
A27
Nom Size=
MaterialSch=
d=
D=
f=
fr=
6 in
ASS CS
40
6.065 in
0.5054 ft
0.0225
0.0150
and fittings
pipe ID
pipe IDfriction f,
Ref4 (Estimated quantities below)
K values based in pipe size and schedule
Qty Component
3000 pipe
2 ball valve (full port)
53 ell-90 deg-LR (r/d=1.5)
2 tee-run
1 tee-branch
1 enlarger 6"x3" (gradual reducer)
1 enlarger3"x2" (gradual reducer)
K Calc-Reducer 6"x3" schedule 40
Refl A-27 Equations for determining reducer & enlargement Ks
where: dl=smaller pipe ID; d2=larger pipe ID (in)
L/D/unit forfy K(ea) K(Total)
Note 4
Note 4
Refl
Refl
Refl
Ref7
Ref7
2-7 Eqn2-4
A-29
A-30
Pg3-113
Pg3-113
(See K calculation below)
(See K calculation below)
K=fL/D
K=3fT
K-14fT
K=20f
K=60f
1.9786
3
1420
60
0.0225
0.0150
0.0150
0.0225
0.0225
0.0445
0.0450
0.2100
0.4500
1.3500
2.3899
4.5847
133.56
0.09
11.13
0.90
1.35
2.39
4.58
resistance coefficient (total) K=| 154.001
Refl
Refl
Ref6
First calculate angle theta (9)Reducer/Enlargersize:
B-13/14 dl(nom)=
B-13/14 d2(nom)=
Chart 1=
3 in
6 in
5.5 in
dl= 3.068 in
d2= 6.065 in
length (end-end)
let: 1= adjacent side
0= opposite side=(d2-dl)/2
h= hypotenuse
Using Pythagorean theorem (a2 + b2 = c2)
then: h2=12+o2
0= 1.4985 in
h= 5.7005 in
sin(6/2)= o/hsin(9/2)= 0.262872
(Q/2)= 0.265997 radians
(Q/2)= 15.2 degrees(9)= 30 degrees
(6)=<45degrees | YES |
Then from:
Refl A-270.8 sm^-(I-/?2) K,
^1)="—"2^ ")=^- resistance coefficient (larger dia pipe)
Where:
KzfFl)^ K;,(Formulal)
P= ratio of diameters of the smaller to larger pipe
subscript l=smaller end; subscript 2=larger end
Calculation-NG Supply-Pressure Drop 1-Longest Run (2019-0213) Page 6 of 19
letting :
then:
Calculate P:
2-12 Eqn2-28
A=
A=
p=
the constant
0.8
(areal/area2)°-5=(dl/d2)Refl
P= 0.5059
solving: K2<F1)= 2.3899 resistance coefficient (larger dia pipe)
from above: 1<2(F1)= Ki/(34
then: Ki= KZ (F1)(P4) resistance coefficient (smaller dia pipe)
solving: l<i= 0.1565 resistance coefficient (smaller dia pipe)
K Calc-Reducer 3"x2" schedule 40
Refl A-27 Equations for determining reducer& enlargement Ks
where: dl=smaller pipe ID; d2=larger pipe ID (in)
First calculate angle theta (6)
Reducer/Enlarger size:
Refl B-13/14 dl(nom)= 2 in dl- 2.067 in
Refl B-13/14 d2(nom)= 3 in d2= 3.068 in
Ref6 Chart 1= 3.5 in length (end-end)
let: 1= adjacent side
0= opposite side=(d2-dl)/2
h= hypotenuse
Using Pythagorean theorem (a + b = c )
then: h2=12+o2
0= 0.5005 in
h= 3.5356 in
sin(6/2)= o/hsin(Q/2)= 0.14156
(6/2)= 0.142037 radians
(6/2)= 8.1 degrees(9)= 16 degrees
(9)=<45degrees | YES |
Thenfrom:.__ 0.8 sin^ (l-/^) ^Refl A-27 K^Ff} = —^——:——')= '— resistance coefficient (larger dia pipe)
p* •' p4
Where:
K2(F1)= ^(Formulal)
P= ratio of diameters of the smaller to larger pipe
subscript l=smaller end; subscript 2=larger end
letting :then:
Calculate?:
2-12 Eqn2-28
solving:
A=
A=
p=
p=
K,(F1)-
the constant
0.8
(areal/area2)°'5-(dl/d2)
0.6737
0.3002
Refl
resistance coefficient (larger dia pipe)
from above: 1<2(F1)= Ki/P4
then: Ki= K; (Fl)((3'>) resistance coefficient (smaller dia pipe)
solving: Ki= 0.0619 resistance coefficient (smaller dia pipe)
Calculation-NG Supply-Pressure Drop 1-Longest Run (2019-0213) Page 7 of 19
Convert calculated K^ (larger dia of reducer) to 1< relative to 6-in piping
Refl 2-9Eqn2-9 K.= ^ [(d^/dt,)4]
Where:
d= inside diameter
subscript a relates to size with reference to which all resistances are to be expressed
subscript b relates to any other size
therefore: a=6" pipe and b=3"pipe
from above: dg= 6.065 in for 6" pipe
d[,= 3.068 in for 3" pipe
K;,(Fl)=Kb= 0.3002 for 3" pipe
solving: Kg= 4.5847 for 6" pipe
Calculate Equivalent Length (Le) from K (total)
fLRefl 2-7 Eqn 2-4 K=
DResistance coefficient (ft/ft)
where:
f= friction factor (unitless)
L= length of pipe (ft)
D= internal diameter (ft)
then:
from above:
solving:
Le=L=
K=
D=
f=
Le=
KD/f154.00
0.5054
0.0225
3459
ft
ft
ft
Ktotal
Friction factor (f) check (compare calculated f to Moody chart lookup value)
Calculate friction factor f using Swamee-Jain formula:
Refl
Refl
6-2 Eqn6-7 f=0.25
£ , 5.74 \V.[lo9[3^D+-R^
Friction factor (unitless)
for: 5000< Re <3xlOA8, 10A-6< e/D <0.01
where:
e= absolute roughness (ft)
D= internal diameter (ft)
Re= reynolds number (unitless)
A-24
from above:
from above:
solving:
from above:
E=
D=
6/D=Re=
f=
0.00015
0.5054
0.000297
4.46E+04
0.0224
0.0225
ftft2.97E-04
commercial steel
meets criteria
from Moody Chart%error= -0.44% calculated factor vs chart factor
Calculation-NG Supply-Pressure Drop 1-Longest Run (2019-0213) Page 8 of 19
Calculation: Natural Gas Supply-Pipe Pressure Drop Calculation 1-Longest Run
Attachment A
Ref2 Internet-Engineering Toolbox-Liquids, gases and vapors - suggested fluid velocities in pipes
http://www.engineeringtoolbox.com/ftuid-velocities-pipes-d_1885.html
Ref3.1 Project SOW
Ref3.2 NG Consumption (Handout at 12/20/18 meeting-draft)
Ref3.3 ATMOS ENERGY Gas Chemistry Report dated 12/11/18
Ref4 Sketch (20181221KLK)
Ref5 Internet-GlobalSpec-Gas Density and Specific Volume Calculator
http://www.globalspec.com/calculators/gas-density
-Printoutl (NG density at GOpsig 70F)
-Printout6 (NG density at Opsjg 60F)
Ref6 Reducer dimension chart
Ref7 Cameron Hydraulic Data - 16th Addition, 2nd Printing 1981
Page 9 of 19
Fluid Velocities in Pipes Page 1 of 2
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F I uid Velocities in Pipes
Liquids, gases and vapors -su^
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Velocity
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Page 10 of 19
http://www.engineeringtoolbox.com/fluid-velocities-pipes-d_l 885.html 12/1/2014
PERFORMANCE STATEMENT OF WORKDESIGN OF A NATURAL GAS UNE USING EXISTING MTKOGEN LINES
1.0 Description ofServices/Introduction: Four Rivers Nuclear Partnership, LLC, hereinafter referredto as the Contractor, is soliciting a bid for subcontracted engineering services to provide completedesign of natural gas piping to support installation of new heating equipment (i.e. boilers, gasheaters, etc.) for HVAC that wiU be located at C~ 100, C-200/205 and C-300. Natural gascurrently services five (5) package boilers on the east side ofC-600, however, new HVAC servicereplacement equipment will require natural gas supply to the areas mentioned above and notcurrently serviced by natural gas. Additionally, the Contractor requires the design of the naturalgas piping to use existing nitrogen piping, where applicable. An evaluation is currently beingcompleted to verity that the existing nitrogen line is suitable for reuse. This evaluationencompasses both integrity and thickness checks of the exiting line and well as a seismicevaluation. The evaluation will provide background study for use of the existing sections of Aenitrogen line to be repurposed for use as a natural gas line and in compliance with NFPA 54,ASME B31.8, and ASME B3 IE.
The subcontracted engineering firm shall use this evaluation, along with Contractor's conceptualrouting of the new natural gas line (provided in this Performance Statement of Work, see figures 1,
2, & 3) and all applicable codes and standards to complete the Work. Currently, design isunderway for new equipment installations at the C-100 complex and gas demand and volume isknowiL Exact demands for C-200/205 and C-300 are not known at this time, but can beapproximated. The Contractor does not expect a larger demand on the natural gas supply thanwhat it is currently designed to be available. The Contractor will provide the subcontractor withthis information as the information becomes available and will expect the subcontractor to workwith other Contractor subcontractors and suppliers as needed to collect design information. At thecompletion of this design, new equipment installed at C-100, C-2007205 and C-300 shall beserviced by the new gas supply.
The vendor or supplier, hereinafter referred to as the subcontractor, shall provide all requiredengmeering disciplines, equipment, supplies, facilities, transportation, tools, materials,supervision, and other items and non-personal services necessary to perform engineering design
services for natural gas piping desigp in support ofHVAC installation projects as defined in thisPerformance Statement of Work.
General project design considerations: Existing valve replacements or removal, removal/air gapfrom existing facilities that will be non-users of the natural gas service, new pipe construction andsupports, existing pipe supports with additional restraining to design for seismic rating,underground pipe runs of new construction to C~ 100 complex, potential for gas meters design,venting for operational maintenance, additional valves for isolations and pressure relief valves,grade of existing pipe (nitrogen piping 2-inch and greater is seamless or lap welded black steel,schedule 40, ASTM A53 carbon steel), grade of new construction pipe, coating material for pipingand supports, and other necessary design requirements. " - .
General Natural Gas service consideration: Existing supply line is 6 inch, underground service tothe existing package boiler location, pressures vary from 58-67 psig, overpressure protection fromthe supplier, natural gas supply is considered dry, vent location exists at the package boilerlocation. „/
^___ ___„ -..-..... . ..^._... ,^..^—--•- .. .. ..,_,.,. ...^^-^..—.•.^--^
2.0 Specific tasks: Subcontractor shall provide:
• 60%/90%/CFC Design Packages for Contractor review and approval
o Design packages shall be prepared by subcontractor using subcontractor designprocesses and procedures. Drawings shall be generated using the Contractor'sdrawing template in AutoCAD, Design packages shall contain design drawingsand specifications that provide complete and thorough instructions for allfabrication, construction, testing procedures and acceptance requirements for acomplete, safe and acceptable installation meeting all applicable codes andstandards and Contractor and industry requirements. The 60%/90% designpackages shall include appropriate level of design detail that matches the percentcomplete progression expected as agreed to by the Contractor project team. The
2 //(ei-s. I
Page 11 of 19
7
F&M r^r/y Af /2y4>/^ 5c^^
Estimates on natural gas consumption (maximum)
Natural gas cost $5.3174/mcf
BuildingC-757
C-752-A
C-600
C-100 Complex
C-200
C-300
TOTAL
Description
Gas Powered Heaters (UH-1 and UH-2)
Qty 5-107,900 BTU/hr
Qtyl-45,650 BTU/hr
Gas Powered Heaters (2 heaters)
Assume same as C-757 (until I can confirm)
Packaged Boilers (19,500 Ibs/hr steam each max, and 2 used max)
Assume 15,000 Ibs/hr max use
This may get decreased with installation at 100/200/300
New hot water boilers
New heating equipment (may be reduced by electric heat install)
New hot water boilers
BTU/hr
5395001456501
585,150
15,000,000
6,000,000
2,250,000
750,000
cfm
8.9|
0.8|
9.7|
247.5|
99.0|
37.1|
12.4|
MCF/day
415.4|
131
14
356
1435318
598
Cost/day
$$$$
$
$$$
$
686
74
1,895
75828495
3,180
MCF/month
38533
417
10,693
4,277
1,604
535
17943
DRAFT
Page 12 of 19I f?ep 5.z
"^
Current Report
Device ID: 82055Location: Location of Stream 1
Stream: JOP 36
Cal Date: 12/11/2018Cal Time: 9:59:00
Signature:
Detector-t-
Comrt62409355347848286341224734163227101720040212978759171-11444.82059
0.
C1
C 02JL
C2
00 50.00 100.00 150.00 200.00 250.00BBF: 112 - C2 Device: 82055 Date: •I2.-I1/2018 09:26:04
Seconds
DetectorCount
1259565111145096333581521966710451898937087422275974643-73472
-2215870
C2-
C3 109C4
fi "PTIC5 NC5
U-+-4-L
00 50.00 100.00 150.00 200.00 250.00BBK: C3 - C6+ Device: 82055 Date: 12.>-M.'2018 09:26:04
Seconds
Components
PropaneHydrogen Sulfide
IsoButaneButane
NeoPentaneIsoPentane
Pentane
Hexane+
NitrogenMethane
Carbon DioxideEthyleneEthaneHexaneHeptaneHeptaneOctane
Nonane
Nonane'
Decans
Undecane
Ethane-
' Propane +
OxygenWater
HeliumHydrogen
&^S-ft3iU<p'AcTiOS.
RF2.745560,000002.033308.835190.000000.357391.708570.226863.353021.300051.418750.000001.027570.000000.000000.000000.000000.000000.000000.000000.000000.000000.000000.000000.000000 000000.00000
Contract Settings
2843190
2577139288
09576114438764
5702811169939840
10525310
1515823700000000
145211568433134
0000
Unnormalized0.084600.000000.006170.009270.000000.002080.002440.001641.76173
92.586720.404160.000004.645320.000000.000000.000000.000000 000000.000000.000000.000000,000000.000000.000000.000000.000000.0000099.50413
Normalized0:085030.000000.006200.009310.000000.002090.002460.001651.77050
93.048120.406180.000004.668470.000780.000000.000580.000280.000000.000000.000000.000000.000000.000000.000001.740670.000000.00000
101.74232
cy2.139350.000000.201700.303840.000000.08347•0.09845
0.000000.00000
939.786010.000000.0000082.617840.037160.000000.032010,017690.000000 000000.000000.000000,000000.000000.000000.000000.000000.00000
Calculated Results
.,iaui€s_.
0.023470.000000.002030.002940.000000.000760.000890.000000.1951615.804480.069450.000001.250900.000320.000000.000270.000150.000000.000000.000000.000000.000000.000000.000000.000000.000000.0000017.35082
SG0.001290.000000.000120.000190.000000.000050.000060.000000.017120.515400.006170.000000.048470.000020.000000.000020,000010.000000.000000 000000.000000.000000.000000.000000.000000.000000.00000
Pressure: 14.73000 psinTemperature: 60.00000 deg F
Humidity: 100%Contract Hour: 0
Ideal CV; 1025.31750 Btu/SCF 6'7~^ Superior Wobbe: 1340.83398 Btu/SCFSuperior CV: 1029.90649 Btu/SCF RiZ.y Inferior Wobbe: 1316.87585 Btu/SCF ^ .. . ,»Inferior CV: 1012 01764 Btu/SCF t0e+-Relative Density: 0.58999 Ibm/tU •s? ^€0-'^^- ^^
Compressibility: 0.99785 Normal Density: 0.04515 lbm/tt3Methane Number: 95.77462 Speed of Sound: 427.25092 m/s
Page 13 of 19 /jf!EE^U
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Results
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OBOOKNftRK gifcE3.
Below are the results of your calculation. To run a different calculation, you may change yourvalues on the form betow and resubmit-
Density:
Specific Volume;
0.256 Ib/ft
3.902 ft'/lb
Pressure: (psig)
Temperature: (F)
Compressibility Factor: (Hsia)
^Molecular Weight: (Ib/lbmol) (Typical vstues)/'**
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Page 15 of 19
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Engineering 360Csteutetor
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UW~TOP
calculations is:
PV = nZRT
This equation is sometimes reThis caiculator has been scale
weights for acetylene; air, amrhydrogen, natural gas» nitrogeEngineering Calculator Disclai
Pressure: (psig)
Temperature: (F)
Compresstbility Factor (HC^)
Molecular Weight (INIbmd)
Reference Library ^ Search Reference Library
Typical Molecular Weight Values
ACETfLENE
AIR
AMMONIA
ARGON
CARBONDIOXIDE
CARBONMONOXIDE
CHLORINE
HYDROGEN
26ib/lbmol
29Sb/lbmol
17Sb/lbmol
39.9Ib/Ibmo!
44Ib/lbmol
28Ib/Sbmol
70.9
!b/ibmol
2Sb/lbmol
NITROGEN28ib/lbmol
^D^^\V^lnfi&
Gas Density and Specific Volume Calculator at GlobalSpec Page 1 of 2
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Gas Density and Specific Volume CalculatorThe Gas Density and Specific Volume Calculator calculates the density and specific volume ofgas based on a modified version of the Ideal Gas Law;
PV=nRT where:P is the absolute pressure of the gas,V is the volume of the gas,n is the number of moles of gas,T is the absolute temperature of the gas,R is the universal gas constant
The Ideal Gas Law assumes the existence of a gas with no volume and no interactions withother molecules. Therefore, the Compressibility Factor (Z) can be used for a slight alteration tothe ideal gas law to account for real gas behavior. Therefore the equation used for thesecalculations is:
PV = fiZRT where:P is the absolute pressure of the gas,V is the volume of the gas,n is the number of moles of gas,T is the absolute temperature of the gas,R is the universal gas constantZ is the gas compressibility factor
This equation is sometimes referred to as the Non-ldeal Gas LawThis calculator has been scaled to use English units for temperature and pressure. Molecularweights for acetylene, air, ammonia, argon, carbon diou'de, carbon monoxide, chlorine,hydrogen, natural gas, nitrogen, oxygen, propane and steam are all provided.Engineering Calculator Disclaimer
.OBOOKMRRK B " B.,Results
Toshiba MotorControl Products -
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Until April 22nd
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Below are the results of your calculation. To run a different calculation, you may change yourvalues on the form belcw and resubmit.
Density:
Specific Volume:
0.051 Ib/ft'
19.452 ft3/lb
Pressure: (psig)
Temperature: (F)
Compressibility Factor (Help)
Molecular Weight; (Ib/lbmol) (Typical values)
p
^0-_
'1
[fsTif
I Submit | j Reset |
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Page 17 of 19
https://www.globalspec.com/calculators/gas-density
f^i»4-ToaT"<p
2/13/2019
FITTINGS
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NFS
1<23/4
1r/4r/22
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.8401.0501.3151.6601.9002.3752.87S3.5004.0004.5005.5636.6258.62510.75012.75014.00016.00018.00020.00024.00030.00036.00042.000
~Qu-s
w.
.OE
.06
.1C
.1C
.1C
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250?50250312312312375i75sOO500
SCH30
.277
.307
.330
.375
.375.438.500.562.625.625
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STD
.109
.113
.133
.140
.145
.154
.203216.226
237258-280.322.365.375.375.375.375.375.375.375.375.375
SCH40
.109
.113
.133
.140
.145
.154203.216.??fi
.237
.258-280.322.365.406.438.soo.562,594.668
.750
WAUL THICKNESS
SCHGO
.406
.500
.562
.594
.656
.750
.812
.969
.147
.154
.179
.191
.200218.276.300.318.337.375.432.500.500.500.500.500.500.500.500.500.500.500
SCHso
.147
.154
.179
.191200,218276.300.318.337.375.432.500.594.688.750.844.9381.0311.219
ONC •AOIUS*»Ktt-i
SCH100
.594
.719
.844
.9381.0311.1561.2811.531
SCH120
.438
.500-562.719.8441.0001.0941.2191.3751.5001.812
SCH140
.8121.0001.1251.2501.4381.5621.7502.062
SCH160
..188
.219250.250.281.344.375.438
.531
.625
.719
.9061.1251.3121,4061.5941.7811.9692.344
XXStg
.294.308.358.382.400.436.552.600.636
.674
.750
.864
.S751.0001.000
A
1'/2
r/a11/217/.21/,333/44'/25V<67',291215182124273036455463
II
B
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111/<r/222'/23
'2
4568101214
Note: Fittings are standard with full openings.
Fittlnfl
l."<-':' T'. '7v..fi'^:vr'xfn'r~°^.
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Plug Valve branch-flo
Standard albow
longradiusso"
UD
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(fl^
30
Nominal pipe size
m 2t/z-3 8-10 | 12-16 | 18-24
K value
^
0.81
2.43 2.25
0.40
0.41
0.35
1.89
0.86
0.30
0.81
1.62
0.29
0.31
0.51
0.27
0.68
0.27
0.45
0.63
0.25
0.42
1.26
0.22
0.23
0.39
1.17
0.39
0.21
?w
I3 "?2 ?• 3*® 0 2:
I?!-I s &Iw
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w S'S 35" "O
I?7S
Mlo I '2
?a:
c<pA
(0
0,30
0.19
0.19
@s3Di?0
IIIx
s?\
Calculated from data in Cram Co; Technical Paper No. 410.
Note: Fittings are standard with full openings.
w
Fitting
Closa Return Bend
r.\Standard Tee
-J L,
90° Bends. Pipe bends, Hangedelbows, butt welded elbows
A,'r/
dJ "
Mltrs Bends
—d-
^^^"
Type ofbend
thru flo
thru branch
r/d= 1
r/d= 2
r/d- 3
r/d= 4
r/d= 6
r;d= 8
r/d=10
r/d == 12
r/d = 14
r/d = 16
r;d=-18
r/d == 20
0°
a » 15°
a « 30°
a =45°
a =60°
u=7S°
a =90°
L/D
50
20
60
20
12
1214
17
24
30
34
38
42
46
so
2
4
8
15
25
40
60
Nominal pipe size
'',2
1.35
0.54
1.62
0.54
0.32
0.32
0.38
0,48
0.65
0.81
0.92
1.03
1.13
1.24
1.35
0.05
0.11
0.22
0.41
o.es
1.09
1.62
V4
1.25
0,50
1.50
0.50
0.30
0,30
0.35
0.43
0.60
0.75
0.85
0.95
1.05
1.15
1.25
0.05
0.-10
0.20
0.38
0.63
1.00
1.50
1
1.15
0,46
1.38
0.48
02S
0.28
0.32
0.39
0,55
0.69
0.78
0.87
0.97
1.06
1.15
0.05
0,09
0.18
0.35
0.58
0.92
1,38
iv<
1.10
0.44
1.32
0.44
0.26
0.26
0.31
0.37
0.63
0.66
0.75
0.84
0-92
1.01
1.10
0.04
0.09
0.18
0.33
0.55
0.88
1.32
11A
1.05
0.42
1.26
0.42
0.25
0.25
0.29
0.36
0,50
0.63
0.71
0.80
0.88
0.97
1.05
0,04
0,08
0.17
0.32
0.53
0.84
1.26
2
0.95
0.38
1.14
0.38
0.23
0.23
0.27
•0.32
0.46
0.57
0.85
0.72
0.80
0.87
0.95
0.04
0.08
0.15
.0.29
0.48
0.76
1.14
2^-3
value
0.90
0.36
1.08
0.36
0.22
0.22
0.25
0.31
0.43
0.54
0.61
0.68
0.76
0.83
0.90
0.04
0.07
0.14
0.27
0.45
0.72
i.oa
4
0,85
0.34
1.02
0.34
0.20
0.20
0.24
0.29
0.41
0.51
0.58
0.65
0.71
0.78
0.85
0.03
0.07
0.14
0.26
0.43
0.68
1.02
6
0.75
0.30
0.90
0.30
0.18
0.18
0.21
0.26
0.36
0.45
0.51
0.57
0.63
0.69
0.75
0.03
0.06
0.12
0.23
0.38
0.60
0.90
8-10
0,70
0.28
0.84
0.28
0.17
0.17
0.20
0.24
0.34
0.42
0.48
0.53
0.59
0.64
0.70
0.03
0.06
0.11
0,21
0.35
0.56
0.84
12-16
0.65
0.26
0.78
0,26
0.16
0.16
0.18
0.22
0.31
0.39
0.44
0.49
0.55
0.60
0.65
0.03
0,05
0,10
0.20
0.33
0.52
0.78
18-24
0.60
0.24
0.72
0.24
0.14
0.14
0.17
0.20
0.29
0.36
0.41
0.46
0.50
0.55
.0.60
0.02
0.10
0.18
0.30
0.48
0.72
r»3.
S ipmiQ.<Ba
^cs303aa=F
11^
<s?b
03r-0w<fl®w
35"0<t»"n
?3(0co
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0§?*5'
IA
I!sn
§
Im3>-a
nm
@01Calculated from data in Crane Co. Technical Paper No, 410,
Page 19 of 19 \^Yrl ,
