IDP PROJECT REPORT

Design of Heat Exchanger for Waste Heat Utilization from Exhaust Gases of Furnace

B.H.GARDI COLLEGE OF ENGINEERING & TECHNOLOGY Page 1

Chapter-1 Introduction

A Heat Exchanger Is A Device That Is Used To Transfer Thermal Energy (Enthalpy)

Between Two Or More Fluids, Between A Solid Surface And A Fluid, Or Between Solid

Particulates And A Fluid, At Different Temperatures And In Thermal Contact. In Heat

Exchangers, There Are Usually No External Heat And Work Interactions. Typical Applications

Involve Heating Or Cooling Of A Fluid Stream Of Concern And Evaporation Or Condensation

Of Single- Or Multicomponent Fluid Streams.

In Other Applications, The Objective May Be To Recover Or Reject Heat, Or Sterilize,

Pasteurize, Fractionate, Distil, Concentrate, Crystallize, Or Control A Process Fluid. In A Few

Heat Exchangers, The Fluids Exchanging Heat Are In Direct Contact. In Most Heat Exchangers,

Heat Transfer Between Fluids Takes Place Through A Separating Wall Or Into And Out Of A

Wall In A Transient Manner. In Many Heat Exchangers, The Fluids Are Separated By A Heat

Transfer Surface, And Ideally They Do Not Mix Or Leak. Such Exchangers Are Referred To As

Direct Transfer Type, Or Simply Recuperates. In Contrast, Exchangers In Which There Is

Intermittent Heat Exchange Between The Hot And Cold Fluids—Via Thermal Energy Storage

And Release Through The Exchanger Surface Or Matrix Are Referred To As Indirect Transfer

Type, Or Simply Regenerators. Such Exchangers Usually Have Fluid Leakage From One Fluid

Stream To The Other, Due To Pressure Differences And Matrix Rotation/Valve Switching.

Common Examples Of Heat Exchangers Are Shell-And Tube Exchangers, Automobile

Radiators, Condensers, Evaporators, Air Preheaters, And Cooling Towers. If No Phase Change

Occurs In Any Of The Fluids In The Exchanger, It Is Sometimes Referred To As A Sensible

Heat Exchanger. There Could Be Internal Thermal Energy Sources In The Exchangers, Such As

In Electric Heaters And Nuclear Fuel Elements. Combustion And Chemical Reaction May Take

Place Within The Exchanger, Such As In Boilers, Fired Heaters, And Fluidized-Bed Exchangers.

Mechanical Devices May Be Used In Some Exchangers Such As In Scraped Surface Exchangers,

Agitated Vessels, And Stirred Tank Reactors.

Heat Transfer In The Separating Wall Of A Recuperate Generally Takes Place By

Conduction. However, In A Heat Pipe Heat Exchanger, The Heat Pipe Not Only Acts As A

Separating Wall, But Also Facilitates The Transfer Of Heat By Condensation, Evaporation, And

Conduction Of The Working Fluid Inside The Heat Pipe. In General, If The Fluids Are

Immiscible, The Separating Wall May Be Eliminated, And The Interface Between The Fluids

Replaces A Heat Transfer Surface, As In A Direct-Contact Heat Exchanger.

A Heat Exchanger Consists Of Heat Transfer Elements Such As A Core Or Matrix

Containing The Heat Transfer Surface, And Fluid Distribution Elements Such As Headers,

Manifolds, Tanks, Inlet And Outlet Nozzles Or Pipes, Or Seals. Usually, There Are No Moving

Parts In A Heat Exchanger; However, There Are Exceptions, Such As A Rotary Regenerative

Exchanger (In Which The Matrix Is Mechanically Driven To Rotate At Some Design Speed) Or

A Scraped Surface Heat Exchanger. The Heat Transfer Surface Is A Surface Of The Exchanger

Core That Is In Direct Contact With Fluids And Through Which Heat Is Transferred By

Conduction. That Portion Of The Surface That Is In Direct Contact With Both The Hot And Cold

Fluids And Transfers Heat Between Them Is Referred To As The Primary Or Direct Surface.



To Increase The Heat Transfer Area, Appendages May Be Intimately Connected To The

Primary Surface To Provide An Extended, Secondary, Or Indirect Surface. These Extended

Surface Elements Are Referred To As Fins. Thus, Heat Is Conducted Through The Fin And

Convected (And/Or Radiated) From The Fin (Through The Surface Area) To The Surrounding

Fluid, Or Vice Versa, Depending On Whether The Fin Is Being Cooled Or Heated. As A Result,

The Addition Of Fins To The Primary Surface Reduces The Thermal Resistance On That Side

And Thereby Increases The Total Heat Transfer From The Surface For The Same Temperature

Difference. Fins May Form Flow Passages For The Individual Fluids But Do Not Separate The

Two (Or More) Fluids Of The Exchanger. These Secondary Surfaces Or Fins May Also Be

Introduced Primarily For Structural Strength Purposes Or To Provide Thorough Mixing Of A

Highly Viscous Liquid.

Not Only Are Heat Exchangers Often Used In The Process, Power, Petroleum,

Transportation, Air-Conditioning, Refrigeration, Cryogenic, Heat Recovery, Alternative Fuel,

And Manufacturing Industries, They Also Serve As Key Components Of Many Industrial

Products Available In The Marketplace. These Exchangers Can Be Classified In Many Different

Ways. We Will Classify Them According To Transfer Processes, Number Of Fluids, And Heat

Transfer Mechanisms. Conventional Heat Exchangers Are Further Classified According To

Construction Type And Flow Arrangements. Another Arbitrary Classification Can Be Made,

Based On The Heat Transfer Surface Area/Volume Ratio, Into Compact And Non-Compact Heat

Exchangers. This Classification Is Made Because The Type Of Equipment, Fields Of

Applications, And Design Techniques Generally Differ.

1.1 Problem Summery

We Have Defined Our I.D.P Project As Energy Conservation And Co Generation From

An Annealing Oil Furnace In Which The Furnace Is Working At 900 °C To 1100 °C. And The

Exhaust Flue Gasses Is Leaving From Furnace At 400 °C-500 °C.

The Phosphating Line Consist Of 13 Chemical Tanks and Water Rains In Which 5 Tanks

Require Certain Temperature For Working Condition Of Chemicals. To Heat Up That Tanks

Between 65-70 °C Each Tank Carry 12 Heater. Which Carry Huge Consumption Of Electricity

Of Overall Plant.

Fig.1 Process Layout of Cold Forging Plant

Raw Material

Softening Cutting Shot

Blasting

PhosphatingWater Rinse

Acid Rinse

Phosphate Neutralizer Soaping Drying

Cold Forging

Cold Forging

Heat Treatment

Annealing Normalizing Shot Blasting

Machining



To Overcome From This Situation We Are Designing Two Heat Exchanger One From

Hot Flue Gases To System Fluid And Another Heat Exchanger From System Fluid To Chemical

Tanks. Due To This Project We Can Utilize That Waste Flue Gases Heat Energy To Heat Up

That Chemical Tank.

1.2 Selection Of Project

We Define Our Project Definition In Our Summer Internship 2015. Over There We Have

Taken Our Industrial Training In Echjay Industries Pvt. Ltd. In Our Internship Over There We

Have Visited Whole Industries & We Find Different Departments. In There One Of The

Department Is “Cold Forging” Unit.

During The Visit Of Cold Forging Unit We Have Observed That In Phosphating Line

There Several Chemical Tanks Which Require A Certain Temperature To React With Object. So

To Heat Up That Tanks They Are Using Twelve Electric Heaters Per Tank Which Consume

More Amount Of Conductive Electricity. The Power Factor Of Electricity Is 0.67 To 0.7. And

We Observed That There Is An Annealing Furnace Which Is Situated Beside The Phosphating

Line. It Is Use For Heat Treatment Of Work Piece To Remove The Internal Stresses And Increase

Malleability & It Has A Temperature Range Of 900-1100 ͦC.

So We Have Suggested That Rather To Heating The Phosphating Line By Use Of Electric

Heater We Can Use Utilize The Temperature Of Flue Gases Coming From The Exhaust Of

Furnace. By Putting A Heat Exchanger We Will Transfer Exhaust Temperature To Phosphating

Tank. Due To This We Can Reduce The Electric Consumption And Increase The Plant

Efficiency.

Fig.2 Flow Process Of Cold Forging



1.3 Objectives & Aims.

1. Industry

As The Industry Is Using Electric Heater Its Overall Energy Cost Increases Due

To Which Production Cost Is Also Increases.

By Utilizing This Exhaust Heat Of Flue Gases Use Can Reduce The Energy Cost

& Increase The Profit.

By Doing This Energy Conservation Project And After The Implementation The

Market Value Of Industry Is Increase Due To Energy Saving Projects.

By Implementing This Kind Of Projects Industry Can Achieve Some Good

Environment Friendly Rewards And Good Quality Standards. I.E. Iso 14000, Iso

9000/4000.

2. Society

With The Help Of This Project We Can Utilize The Heat Which Is Directly

Emitted To Atmosphere Which Will Affect The Surrounding The Ecosystem.

By Utilizing That Heat In Place Of 12 Electric Heater Per Tank Which Will

Reduce The Power Consumption. So The Overall Total Consumption Load Of

Industry Is Reduce Due To Which The Government Can Utilize That In Different

Power Grid.

This Project Will Create An Awareness Of Power Saving To The Employer And

Worker.

1.4 Problem Specification

In Forging Industry, Particularly In Cold Working Process The Raw Material Are

Cleaned & Soaped By Chemicals Which Is Heated At Particular Temperature. The Heat Is

Supplied By Electric Heaters. The Furnace For Heat Treatment Process Is Situated Besides The

Phosphating Plant. By Utilizing The Heat Of The Exhaust Flue Gases Which Is Coming Outside

From The Furnace By Use Of The Heat Exchanger The Utilized Heat Can Be Supply To The

Phosphating Instead Of Electric Heaters. The Power Consumption Of The Electric Heater Will

Decrease. Thus Over All Energy Consumption Will Decrease.



Fig.3 Layout Of Project

Particular Problem Specification Are Listed Under:-

I. Theoretical Design:-

1. Design Of Heat Exchanger From Furnace To System.

2. Design Of Heat Exchanger From System To Chemical Tank.

3. Distribution System.

4. Pumping System.

5. Valve Control System.

6. Temperature Control System.

II. Computational Design:-

1. Modelling.

2. Meshing And Boundary Condition.

3. Simulation.



Chapter-2 Literature Review & Data Collection

2.1 Industrial Data Collection

In The Industry We Have Measured Flue Gases Exhaust Pipe Which Is Over Oil Furnace

And Get The Dimension And Temperature

Furnace Exhaust Pipe OD = 500mm

Furnace Exhaust Pipe ID = 470mm

Refractory Brick = 20mm

Temperature Range = 400-500°C

Flow Rate Of Flue Gases As Per Industrial Guide And As Per Reference Book Studied And

Calculated= 0.6106 Kg/S (Referring Velocity= 10m/S).

No Of Tanks To Be Heated = 5

Capacity Of Tanks = 2700 Litres

Temperature To Maintain In Tanks = 60-75 °C.

Electrical Heating Rods Per Tanks = 12

Capacity Of Each Electrical Heating Rods = 9 Kw 230/400 V

Overall Efficiency Of Pump (𝜂ℎ𝑝) = 80%

2.2 Material Selection

Stainless Steel Specification

The Rate Of Thermal Expansion Of Stainless Steel Remains Relatively Constant Up

To 1200°C Compared To Carbon Steel Because Stainless Steel Does Not Experience

Phase Transformation.

The Magnitude Of Thermal Expansion Of Stainless Steel Is Greater Than The

Thermal Expansion Of Carbon Steel.

The Specific Heat Of Stainless Steel Increases Slightly At Elevated Temperatures,

Compared To Carbon Steel, Which Has A Huge Increase In Specific Heat At 730°C

Due To A Chemical Transformation From Ferrite-Pearlite To Austenite.

At Ambient Temperature, Stainless Steel Has A Much Lower Thermal Conductivity

Compared To Carbon Steel. However, The Thermal Conductivity Of Stainless Steel

Increases At Elevated Temperatures Which Will Exceed The Value Of Carbon Steel

Above 1000°C.



Graph No.1 Specific Heat Vs. Temp. Of Stainless Steel & Carbon Steel

Through This Graph We Can See That The Specific Heat Of Carbon Steel Will Vary With

Respect To Certain Temperature After 650°C The Specific Heat Increases Suddenly Then After

It Will Reduces So Sudden Fluctuation Is There In Carbon Steel While The Specific Heat Of

Stainless Steel Is Consistent In All Temperature Very Little Variation In Larger Temperature

Scale.

Graph No.2 Thermal Elongation Vs. Temp. Of Stainless Steel & Carbon Steel

The Above Graph Is The Representation Of Comparing The Thermal Elongation At

Different Temperature Of Two Different Material, As We Can See The Difference Of Elongation

In This Materials The Carbon Steel Has Less Elongation Compare To Stainless Steel But At The

Same Time The Stainless Steel Have More Strong Property Like Wear Resistance, Corrosion

0

1000

2000

3000

4000

5000

6000

SP

EC

IFIC

HE

AT

(

J/K

G.K

)

TEMPERATURE(℃)

carbon steel Stainless Steel

0

5

10

15

20

25

0 100 200 300 400 500 600 700 800 900 1000 1100 1200

Th

erm

al

Elo

ngati

on

Δ

L/

L (

×10

-3)

Temperature(℃)

Carbon Steel

Stainless Steel



Resistance, More Life Span So Compare To Carbon Steel We Selected Our Initial Material As

Stainless Steel.

Table No.1 Material and Its Thermal Conductivity

Material Thermal Conductivity (W/M.K)

AISI 302 15.1

AISI 304 14.9

AISI 316 46.8

AISI 347 14.1

201 Annealed Steel 16.3

AISI 1015 (Cold Drawn Ss) 52

AISI 4130 42.7

Alloy Steel (Ss) 50

Copper 345

Aluminium 234



Chapter-3 Theoretical Design Calculation

3.1 Theoretical Design Calculations

Theoretical Design Steps:-

Table No.2 Equations Require For Calculating The Heat Transfer Problems

The Overall Heat Transfer Co-Efficient

𝑈𝑜 = 1

𝐴𝑜

𝐴𝑖ℎ𝑖+

𝐴𝑜Ln(𝑟𝑜

𝑟𝑖)

2𝜋𝑘𝐿+

1ℎ𝑜

1

𝑈𝑖=

𝐷𝑜

ℎ𝑖𝐷𝑖+ (

𝐷𝑜

𝐷𝑖× 𝑅𝑓𝑖) +

𝐷𝑜 Ln(𝐷𝑜

𝐷𝑖)

2𝑘+

1

ℎ𝑜

𝑈 = 1

1ℎ𝑖

+ 1

ℎ𝑜

The Heat Transfer Rate

𝑞 = 𝑇𝐴 − 𝑇𝐵

1ℎ1𝐴

+∆𝑥𝑘𝐴

+1

ℎ2𝐴

𝑞 = 𝑈𝐴∆𝑇𝑜𝑣𝑒𝑟𝑎𝑙𝑙

𝑞 = 𝑇𝐴 − 𝑇𝐵

1ℎ𝑖𝐴𝑖

+Ln(

𝑟𝑜

𝑟𝑖)

2𝜋𝑘𝐿+

1ℎ𝑜𝐴𝑜

𝑄 = 𝑚𝐶𝑝∆𝑇



For Unit Length Basis The Thermal

Resistance Of The Steel 𝑅𝑠 = Ln(

𝑟𝑜

𝑟𝑖)

2𝜋𝐾𝐿

For Unit Length Basis The Thermal

Resistance On The Inside

𝑅𝑖 = 1

ℎ𝑖2𝜋𝑟𝑖𝐿

Reynolds’s No. 𝑅𝑒 =

𝜌 × 𝑉 × 𝑑

𝜇

Prandlt’s No. 𝑃𝑟 =

𝐶𝑝 × 𝜇

𝑘

Greyshollf’s No. 𝐺𝑟 =

𝛽 × 𝑔 × 𝐷3 × 𝜌2 × (𝑇𝑠 − 𝑇𝛼)

𝜇2

Logamathric Mean Temperature Difference 𝐿. 𝑀. 𝑇. 𝐷. =

(𝑇ℎ,𝑖 − 𝑇𝑐,𝑜) − (𝑇ℎ,𝑜 − 𝑇𝑐,𝑖)

Ln[ (𝑇ℎ,𝑖 − 𝑇𝑐,𝑜) ÷ (𝑇ℎ,𝑜 − 𝑇𝑐,𝑖)]

Heat Transfer Co-Efficient ℎ =

𝑁𝑢 × 𝐾

𝑑

Nusselt’s No.

𝑁𝑢 =

𝑓2 × (𝑅𝑒) × 𝑃𝑟

1 + 8.1 × 𝑓8

0.5

× [ 𝑃𝑟

23 − 1]

Required Length For Heat Exchanger 𝐿𝑒𝑛𝑔𝑡ℎ =

𝑄

𝜋 × 𝐷𝑖 × 𝑈 × 𝐿. 𝑀. 𝑇. 𝐷.

Pressure Drop (Δp) ∆𝑃 =

4 × 𝑓 × 2 × 𝐿 × 𝜂ℎ𝑝 × 𝜌 × 𝜇𝑚2

𝑑𝑖 × 2

Pumping Work (P) 𝑃 =

1

𝜂𝑝×

�̇�𝑝 × ∆𝑃

𝜌



Theoretical Design Calculation For Heat Exchanger -1

1. Double Pipe Heat Exchanger (Connected In Series)

o Inner Pipe Dimensions

Outer Diameter = 0.12m

Inner Diameter = 0.10m

o Outer Pipe Dimensions

Inner Diameter (Di) = 0.470m

Outer Diameter (Do) = 0.50m

o Cold Fluid Inlet Temperature (Tci) = 40℃

o Cold Fluid Outlet Temperature (Tco) = 95℃

o Hot Fluid Inlet Temperature (Thi) = 300℃

o Inner Cold Fluid (Water) Properties At 65℃

Density 𝜌 = 980 𝐾𝑔

𝑚3

Specific Heat 𝐶𝑝= 4.191 𝐾𝐽

𝐾𝑔.𝐾

Thermal Conductivity K= 0.668 𝑊

𝑚.𝑘

Viscosity = 420 × 10−6 𝑃𝑎. 𝑠

Prandlt’s No. = 2.99

o Outer Hot Fluid (Dry Air) Properties At 200℃

Density 𝜌 = 0.774 𝐾𝑔

𝑚3

Specific Heat 𝐶𝑝= 1.021 𝐾𝐽

𝐾𝑔.𝐾

Thermal Conductivity K= 0.0386 𝑊

𝑚.𝑘

Viscosity = 25.07 × 10−6 𝑃𝑎. 𝑠

Prandlt’s No. = 0.686

o Required Heat Is

𝑄 = 𝑚𝐶𝑝∆𝑇

Q = 553.212 Kw (Kj/S)



Calculations For Hot Fluid (Dry Air)

o Heat Supplied = Heat Observed By Heat Exchanger

o 𝑸 = 𝒎𝒉̇ 𝑪𝒑𝒉∆𝑻 = 𝒎𝒄̇ 𝑪𝒑𝒄∆𝑻

o 𝒎𝒉̇ = 𝒎𝒄̇ 𝑪𝒑𝒄

𝑪𝒑𝒉∆𝑻= 𝟐. 𝟕𝟎𝟗𝟏

𝐾𝑔

𝑠

o Reynolds’s No. = 𝜌 𝑉 𝐷

𝜇 = 2,33,187.953 (∴ 𝑇ℎ𝑒 𝑓𝑙𝑜𝑤 𝑖𝑠 𝑡𝑢𝑟𝑏𝑢𝑙𝑒𝑛𝑡 )

By, Correlation For Fully Developed Turbulent Convection Through Circular Duct

(From Ref.No.3 ) Gnielinski’s Correlation

o 𝑁𝑢 =𝑓

2×(𝑅𝑒)×𝑃𝑟

1+8.1× 𝑓

8

0.5

×[ 𝑃𝑟

23−1]

Where 𝑓 = (1.58 × Ln 𝑅𝑒 − 3.28 )−2

o 𝑁𝑢 = 0.003787836

2×(233187.953)×0.686

1+8.1× 0.003787836

8

0.5

×[ 0.68623−1]

= 𝟑𝟒𝟑. 𝟖𝟒𝟐𝟏

Heat Transfer Co-Efficient Of Hot Fluid

o ℎ𝑜 = 𝑁𝑢 ×𝑘

𝐷 = 110.60

𝑾

𝒎𝟐𝒌

Calculations For Inner Cold Liquid

o Reynolds’s No. = 𝜌×𝑣×𝑑𝑜

𝜇= 𝟕𝟐, 𝟕𝟓𝟓. 𝟔𝟔𝟔 (∴ 𝑇ℎ𝑒 𝑓𝑙𝑜𝑤 𝑖𝑠 𝑡𝑢𝑟𝑏𝑢𝑙𝑒𝑛𝑡)

By, Correlation For Fully Developed Turbulent Convection Through Circular Duct

(From Ref.No.3 ) Gnielinski’s Correlation

o 𝑁𝑢 =𝑓

2×(𝑅𝑒)×𝑃𝑟

1+8.1× 𝑓

8

0.5

×[ 𝑃𝑟

23−1]

Where 𝑓 = (1.58 × Ln 𝑅𝑒 − 3.28 )−2

o 𝑁𝑢 0.004817256

2×(72755.666)×2.66

1+8.1× 0.004817256

8

0.5

×[ 2.6623−1]

= 𝟐𝟕𝟐. 𝟕𝟗𝟐𝟎



o Heat Transfer Co-Efficient Of Inner Fluid

ℎ𝑖 = 𝑁𝑢 ×𝑘

𝐷 = 1822.25

𝑾

𝒎𝟐𝒌

Rfi = 0.000176 𝑊

𝑚2℃ (From Ref.No.3)

Overall Heat Transfer Co-Efficient On The Outside Of The Inner Tubes

1

𝑈𝑓=

𝑑𝑖

𝑑𝑜 × ℎ𝑖+

𝑑𝑖

𝑑𝑜× 𝑅𝑓𝑖 +

𝑑𝑜 × Ln𝑑𝑖𝑑𝑜

2 × 𝑘+

1

ℎ𝑜= 𝟗𝟓. 𝟑𝟖𝟓𝟗

𝑊

𝑚2℃

𝐿. 𝑀. 𝑇. 𝐷. = (𝑇ℎ,𝑖 − 𝑇𝑐,𝑜) − (𝑇ℎ,𝑜 − 𝑇𝑐,𝑖)

Ln[ (𝑇ℎ,𝑖 − 𝑇𝑐,𝑜) ÷ (𝑇ℎ,𝑜 − 𝑇𝑐,𝑖)]= 𝟏𝟏𝟖. 𝟎𝟏𝟒 ℃

Overall Required Heat Transfer Area Can Be,

𝐿𝑒𝑛𝑔𝑡ℎ = 𝑄

𝜋 × 𝐷𝑖 × 𝑈 × 𝐿. 𝑀. 𝑇. 𝐷.= 𝟔𝟓. 𝟎𝟑𝟒𝟔 𝑚

Pressure Drop In Hot Fluid

∆𝑃 =4 × 𝑓 × 2 × 𝐿 × 𝜂ℎ𝑝 × 𝜌 × 𝜇𝑚

2

𝑑𝑖 × 2 = 𝟒𝟗𝟎𝟔. 𝟓𝟐 𝐏𝐚

Required Pumping Work

𝑃 =1

𝜂𝑝×

�̇�𝑝 × ∆𝑃

𝜌= 𝟒𝟖𝟐𝟏𝟖. 𝟓 𝑾



3.2 Making Of Excel Calculation Sheet & Heat Exchanger Parameters

Optimizations

As The Procedure To Calculate The Length Of Heat Exchanger Is Very Much Complex And

We Have Number Of Variable To Optimize The Length So To Reduce The Time Consumption

We Have Make A Type Of User Friendly Program In Excel, In This We Have Mentioned All

The Parameter So Once The User Will Enter The Required Parameter Directly The Software

Will Calculate All The Required Equation And Generate The Result Of Each And Every

Parameter.

The Given Below Table Shows The First Calculation Which We Perform Theoretically

As Above So At The End We Can See That The Value Of Both The Values Are Equal And

Accurate So With The Help Of This Excel Program We Can Generate The Result Easily And

Make Our Calculation Fast So By Trial And Error Method We Started Optimizing The Pipe

Length.

Table No.3 Calculation No.1 Minimum Hot Fluid Mass Flow Rate

Double Pipe Heat Exchanger (Water-Air) Cold Fluid Water Hot Fluid Air

Mass Flow

Rate(Kg/S)

2.4 Mass Flow Rate

(Kg/S)

2.7091

Inner Pipe Material

Thermal

Conductivity

(W/M.K)

19.841

(Stainless Steel)

Tci (℃) 40 Thi (℃) 300

Tco (℃) 95 Tco (℃) 100

(Tco-Tci) (℃) 55 (Tco-Tci) (℃) 200

Inner Pipe Dimensions Outer (Annulus) Pipe Dimensions

I.D. (M) 0.10 I.D. (M) 0.12

O.D. (M) 0.12 O.D. (M) 0.470

O.D/I.D. 1.2 O.D/I.D. 3.91666

Ln (O.D. /I.D.)

0.1823 Ln (O.D. /I.D.) 1.3652

O.D.-I.D. (M) 0.02 O.D.-I.D. (M) 0.350

Cross Sectional Area

(M2)

0.007853 Cross Sectional Area

(M2)

0.16225

Thermal Properties

Density (Kg/M3) 998 Density (Kg/M3) 0.774

Specific Heat

(Kj/Kg.K)

4.191 Specific Heat

(Kj/Kg.K)

1.021



Thermal

Conductivity

(W/M.K)

0.668 Thermal Conductivity

(W/M.K)

0.0386

Viscosity (Pa.S)

0.00042 Viscosity (Pa.S) 0.00002507

Prandlt's No. 2.66 Prandlt's No. 0.686

Heat Exchanger Calculations

Velocity (M/S)

0.311181 Velocity (M/S) 21.58

Reynold's No. 72755.666 Reynolds’s No. 233187.53

Fanning Friction

Factor (F)

0.004817526 Fanning Friction

Factor (F)

0.003787836

(F/2) 0.0024088 (F/2) 0.00189403

(F/2)^1/2 0.049 (F/2)^1/2 0.0435

Nusselt's No. 272.790250 Nusselt's No. 343.75258

Heat Transfer Co-

Efficient (Hi)

(W/M2.K)

1822.25 Heat Transfer Co-

Efficient (Hi)

(W/M2.K)

110.60

Fouling Factor (Rfi)

0.000176 Fouling Factor (Rfo) -

L.M.T.D. (℃) 118.1926

Required Heat Kw, Q Kw (Kj/S)

Q=(Mass Flow Rate)*(Specific

Heat)*(Tco-Tci)

553.212

Overall Heat Transfer Co-Efficient

(W/M2.K)

95.3859

Heat Transfer Area (Ao) M2 49.144

Required Heat Transfer Pipe Length For

1 Tube L (M) 65.0346

For Optimization We Studied About Heat Transfer Parameters E.G.

Hot Fluid Mass Flow Rate

Pipe Material (Thermal Conductivity, Specific Heat)

Hot Fluid Outlet Temperature

Inner Pipe Dimensions (Outer Diameter, Inner Pipe, Pipe Thickness)

Pressure Drop

Fouling Factor



In This We Have Increased The Mass Flow Rate Of The Hot Flue Gases As The Mass Flow

Rate Change The Temperature Of Flue Gases At Outlet Change And Due To That The L.M.T.D

And Overall Heat Transfer Rate Change And That Will Affect In Length Of Heat Exchanger

Pipe (No. Of Pass = 1)

Table No.4 Calculation No.2 Changing In Hot Fluid Mass Flow Rate & As Per That

Change In Hot Fluid Gases Outlet Temperature (Tho) With Other Constant Parameters


Mass Flow

Rate(Kg/S)

2.4 Mass Flow Rate

(Kg/S)

9

Inner Pipe Material

Thermal

Conductivity

(W/M.K)

19.841

(Stainless

Steel)

Tci (℃) 40 Thi (℃) 300

Tco (℃) 95 Tco (℃) 239.7963

(Tco-Tci) (℃) 55 (Tco-Tci) (℃) 61


I.D. (M) 0.10 I.D. (M) 0.12

O.D. (M) 0.12 O.D. (M) 0.470

O.D/I.D. 1.2 O.D/I.D. 3.91666

Ln (O.D. /I.D.)

0.1823 Ln (O.D. /I.D.)

1.3652

O.D.-I.D. (M) 0.02 O.D.-I.D. (M) 0.350

Cross Sectional

Area (M2)

0.007853 Cross Sectional

Area (M2)

0.16225

Thermal Properties


Specific Heat

(Kj/Kg.K)

4.191 Specific Heat

(Kj/Kg.K)

1.021

Thermal

Conductivity

(W/M.K)

0.668 Thermal

Conductivity

(W/M.K)

0.0386

Viscosity (Pa.S)

0.00042 Viscosity (Pa.S)

0.00002507



Velocity (M/S)

0.311688312 Velocity (M/S)

71.66660694

Reynold's No. 72755.666 Reynolds’s No.

774411.002



Fanning Friction

Factor (F)


Factor (F)

0.003037431

(F/2) 0.0024088 (F/2) 0.001518715

(F/2)^1/2 0.049 (F/2)^1/2 0.038970698


Heat Transfer Co-

Efficient (Hi)

(W/M2.K)


Efficient (Hi)

(W/M2.K)

290.4451548

Fouling Factor

(Rfi)

0.000176 Fouling Factor (Rfo)

-

L.M.T.D. (℃) 202.3870005



Heat)*(Tco-Tci)

553.212


(W/M2.K)

205.59


Required Heat Transfer Pipe Length

For 1 Tube L (M) 17.62752835

As We Can See That By Changing The Hot Fluid Mass Flow Rate There Is Change In

The Length Of The Heat Exchanger -1 So We Have Make A Table Through Which We Can

Analysis That At Which Mass Flow Rate The Pipe Length Is More And Visa-Versa.

Table No.5 Changing In Length Of Heat Exchanger Pipe With Respect To Hot Fluid Mass

Flow Rate

Hot Mass Flow

Rate (Kg/S)

Hot Fluid Velocity

(M/S)

Hot Fluid Exhaust

Temperature

(Tho ℃)

Length Of Heat

Exchanger Pipe M

(No. Of Passes-1)

2.7091 21.57244 99.999 65.43

3 23.888 119.38 54.075

3.5 27.87034 145.19 43.1403713

4 31.8588 164.5416 36.5797

4.5 35.833 179.5416 32.1219

5 39.8147 191.6333 28.8226

5.5 43.7962 201.4848 26.36

6 47.77 209.6944 24.3696

6.5 50.96 216.641 22.96196

7 55.74 222.5952 21.38755

7.5 59.722 227.755 20.2369

8 63.7 232.2708 19.2469

8.5 67.68 236.2549 18.3852

9 71.666 239.7963 17.627



It Is Observed That The At Different Mass Flow Rate The Pipe Length Decreases But

The Value Of Hot Gases At Outlet Increases Which Can Create Higher Pumping Work & It Is

Necessary Not To Take The High Mass Flow Rate Due To Which The Outlet Temperature

Increases. So As Per The Observation It Is Advisable To Take The Average Value Of Mass Flow

Rate So We Have Decided 5 Kg/Sec For Further Calculation.

Graph No.3 Mass Flow Rate (Hot Fluid) Vs. Hot Fluid Outlet Temperature

Graph No.4 Mass Flow Rate (Hot Fluid) Vs. Hot Fluid Inlet Velocity

The Value Of The Inlet Velocity Is Directly Proportional To The Mass Flow Rate Of The

Hot Flue Gases The Increase In Mass Flow Rate Will Increase The Velocity. As The Velocity

Increases The Flow Will Be More Turbulent And The Reynolds Number Will Also Increases So

0

50

100

150

200

250

300

0 1 2 3 4 5 6 7 8 9 10

Hot

Flu

id O

utl

et T

emp

rtu

re (

℃)

Mass Flow Rate (Kg/s)

Mass Flow Rate (Hot Fluid) Vs. Hot Fluid Outlet

Temprature

0

10

20

30

40

50

60

70

80

0 1 2 3 4 5 6 7 8 9 10

Hot

Flu

e G

ase

s In

let

Vel

oci

ty

(m/s

)

Mass Flow Rate (Kg/S)

Mass Flow Rate (Hot Fluid) Vs. Hot Fluid Inlet Velocity



It Is Observed That We Cannot Increase More Mass Flow Rate So There By It Is Advisable To

Select The Correct Mass Flow Rate And As Per Above Selection Of Mass Flow Rate That Is 5

Kg/S, Is Favourable For The Calculation.

Graph No.5 Mass Flow Rate (Hot Fluid) Vs. Required Heat Transfer Pipe Length

As Per The Calculation It Is Observed That By Increasing The Mass Flow Rate The Pipe

Length Is Decreasing Initially By Changing The Mass Flow Rate There Is Waste Change In Pipe

Length But After Some Interval The Ratio Of Change In Mass Flow Rate To Pipe Length Will

Reduce So If We Still Increase The Mass Flow Rate The Pipe Length Will Change Very Less.

There Is One Another Parameter Through Which We Can Reduce The Pipe Length That

Is The Inner And Outer Diameter Of The Internal Pipe Passing From The Exhaust Pipe As We

Change The Pipe Diameter We Can Change The Heat Transfer Coefficient Of Outer Surface

Area As The Area Of Heat Transfer Change So We Have Taken The Standard Pipe Size That Is

50mm Internal Diameter And 58mm Of Outer Diameter Having A Thickness Of 4mm.

Table No.6 Changing In Inner Pipe Diameter With Other Constant Parameters


Mass Flow

Rate(Kg/S)

2.4 Mass Flow Rate

(Kg/S)

2.7091

Inner Pipe

Material

Thermal

345 (Copper)

0

10

20

30

40

50

60

70

0 1 2 3 4 5 6 7 8 9 10

Pip

e L

ength

(m

)

Mass Flow Rate (Kg/s)

Mass Flow Rate (Hot Fluid) Vs. Required Heat Transfer

Pipe Length



Conductivity

(W/M.K)

Tci (℃) 40 Thi (℃) 300

Tco (℃) 95 Tco (℃) 100

(Tco-Tci) (℃) 55 (Tco-Tci) (℃) 200


I.D. (M) 0.05 I.D. (M) 0.058

O.D. (M) 0.058 O.D. (M) 0.470

O.D/I.D. 1.16 O.D/I.D. 8.103448236

Ln (O.D. /I.D.)

0.14852005 Ln (O.D. /I.D.)

2.092289684

O.D.-I.D. (M) 0.008 O.D.-I.D. (M) 0.412

Cross Sectional

Area (M2)


Area (M2)

0.170921143

Thermal Properties

Density

(Kg/M3)

998 Density

(Kg/M3)

0.774

Specific Heat

(Kj/Kg.K)

4.191 Specific Heat

(Kj/Kg.K)

1.021

Thermal

Conductivity

(W/M.K)

0.668 Thermal

Conductivity

(W/M.K)

0.0386

Viscosity (Pa.S)


0.00002507



Velocity (M/S)

1.246753247 Velocity (M/S)

20.47803531


260478.6488

Fanning

Friction Factor

(F)

0.004161022 Fanning

Friction Factor

(F)

0.003707602

(F/2) 0.002080511 (F/2) 0.001853801

(F/2)^1/2 0.045612618 (F/2)^1/2 0.043055789


Heat Transfer

Co-Efficient

(Hi)

(W/M2.K)

6483.473668 Heat Transfer

Co-Efficient

(Hi)

(W/M2.K)

249.8405344

Fouling Factor

(Rfi)

0.000176 Fouling Factor

(Rfo)

-



L.M.T.D. (℃) 118.0142275


Q=(Mass Flow Rate)*(Specific Heat)*(Tco-

Tci)

553.212


(W/M2.K)

217.2702403


Required Heat Transfer Pipe Length For 1

Tube L (M) 59.1799167

It Is Observed From The Above Calculations That By Changing The Different Parameter

We Can Reduce The Pile Length So As Per The Sight Constrain At Industry We Are Going With

Following Parameter Inner Pipe I.D.-50mm & O.D.-58mm, Hot Fluid Mass Flow Rate – 5 Kg./S,

Hot Outlet Temperature(Tho)-191.633℃, Inner Pipe Material – Copper (Thermal Conductivity-

345 W/M.K) )

Table No.7 At Inner Pipe I.D.-50mm & O.D.-58mm, Hot Fluid Mass Flow Rate – 5

Kg./S, Hot Outlet Temperature(Tho)-191.633℃, Inner Pipe Material – Copper


Mass Flow

Rate(Kg/S)

2.4 Mass Flow Rate

(Kg/S)

5

Inner Pipe Material

Thermal

Conductivity

(W/M.K)

345 (Copper)

Tci (℃) 40 Thi (℃) 300

Tco (℃) 95 Tco (℃) 191.633

(Tco-Tci) (℃) 55 (Tco-Tci) (℃) 108.37


I.D. (M) 0.05 I.D. (M) 0.058

O.D. (M) 0.058 O.D. (M) 0.470

O.D/I.D. 1.16 O.D/I.D. 8.103448236

Ln (O.D. /I.D.)

0.14852005 Ln (O.D. /I.D.)

2.092289684

O.D.-I.D. (M) 0.008 O.D.-I.D. (M) 0.412

Cross Sectional

Area (M2)


Area (M2)

0.170921143

Thermal Properties




Specific Heat

(Kj/Kg.K)

4.191 Specific Heat

(Kj/Kg.K)

1.021

Thermal

Conductivity

(W/M.K)

0.668 Thermal

Conductivity

(W/M.K)

0.0386

Viscosity (Pa.S)


0.00002507



Velocity (M/S)

1.246753247 Velocity (M/S)

37.79490479


480747.5707

Fanning Friction

Factor (F)


Factor (F)

0.003306254

(F/2) 0.002080511 (F/2) 0.001653127

(F/2)^1/2 0.045612618 (F/2)^1/2 0.040658664


Heat Transfer Co-

Efficient (Hi)

(W/M2.K)


Efficient (Hi)

(W/M2.K)

408.1688094

Fouling Factor

(Rfi)

0.000176 Fouling Factor (Rfo)

-

L.M.T.D. (℃) 176.9758109



Heat)*(Tco-Tci)

553.212


(W/M2.K)

351.4297339


Required Heat Transfer Pipe Length

L (M) 24.39813036

As Per The Optimised Calculation There Is The Calculation For Pump Work As We

Change The Mass Flow Rate We Have To Change The Pump Work So At Different Mass Flow

Rate The Pump Work Will Also Be Different This Are The Different Pump Work At Different

Mass Flow Rate.



Table No.8 Changing In Pump Work, Pressure Drop With Respect To Hot Fluid

Mass Flow Rate

Mass

Flow Rate

(Kg/S)

Tho (℃) Reynold's

No.

Hot Fluid

Friction

Factor ( F

)

Hot

Fluid

Mass

Velocity

(M/S)

Overall Heat

Transfer So-

Efficient

U(W/M2.K)

Hot Fluid

Pressure

Drop (Δp)

Pump

Work (W)

2.7091 99.099

233114.92

07 0.00379 21.57 95.55 4906.52 20204.36

3 119.38 258137 0.00374 23.888 102.43 4956.41 22601.5

3.5 145.19 301159 0.00361 27.87 113.653 5167.436 27490.65

4 164.5416 344182.26 0.00352 31.85 124.19 5571.326 33873.42

4.5 179.5416 387205.3 0.00344 35.833 134.14 6060.873 41456.82

5 191.6333 430228 0.00337 39.8417 134.58 6344.589 48218.5

5.5 201.4848 473251 0.00331 43.762 152.55 7153.651 59804.04

6 209.6944 516274 0.00326 47.77 161.11 7754.269 64825.18

6.5 216.641 559296 0.00322 50.96 169.304 8356.113 82557.51

7 222.5952 602319 0.00317 55.74 179 8979.431 95440.27

7.5 227.755 645342 0.00314 59.722 184.67 9640.779 109904

8 232.2708 688365 0.0031 63.7 184.07 10310.25 125372.2

8.5 236.2549 731388 0.00306 67.8 198.86 10993.61 142036.2

9 239.7963 774411.02 0.00303 71.666 205.58 11700.13 160056.1

Graph No.6 Reynold's No. Vs. Overall Heat Transfer Co-Efficient

0

50

100

150

200

250

0 100000 200000 300000 400000 500000 600000 700000 800000 900000

Over

all

Hea

t T

ran

sfer

Co

-

Eff

icie

nt(

W/m

2.K

)

Reynold's No.

Reynold's No. Vs. Oveall Heat Transfer Co-Efficient



Graph No.7 Hot Fluid Mass Flow Rate (Kg/S) Vs. Hot Fluid Pressure Drop (Pa)

It Is Observed From The Above Graph That Increase In Mass Flow Rate Will Increase

The Pressure Drop Of Hot Fluid As The Mass Flow Rate Increases The Pressure At Outlet Will

Also Increases So The Pressure Difference Of Both The End Will Increases This Will Reduces

The Efficiency Of The System But For Proper Heat Transfer We Have Selected 5 Kg/S. So As

Per That The Pressure Drop Will Be There And For Same There Is Calculation We Have Taken

The Pump Work.

Graph No.8 Velocity (Hot Fluid) M/S Vs. Pressure Drop (Hot Fluid) Pa

0

2000

4000

6000

8000

10000

12000

14000

0 1 2 3 4 5 6 7 8 9 10

Pre

ssu

re D

rop

(H

ot

Flu

id)

(Pa)

Mass Flow Rate (Hot Fluid) Kg/s

Hot Fluid Mass Flow Rate (Kg/s) Vs. Hot Fluid Pressure

Drop (Pa)

0

2000

4000

6000

8000

10000

12000

14000

0 10 20 30 40 50 60 70 80

Pre

ssu

re D

rop

(H

ot

Flu

id)

Pa

Velocity (Hot Fluid) m/s

Velocity (Hot Fluid) m/s Vs. Pressure Drop (Hot Fluid) Pa



In The Above Graph We Can Observe That As The Velocity Increases The Pressure Drop

Will Also Increases As The Velocity Is Directly Co-Relate With The Mass Flow Rate So It Can

Be Understood That The Value Of Mass Flow Rate And Velocity Both Are Similar So More The

Mass Flow Rate Higher The Pressure Drop.

Graph No.9 Reynolds No. Vs. Friction Factor

This Graph Shows Us That By Increasing The Reynolds Number We Can Reduce The

Friction Factor As The Friction Factor Reduces The Overall Heat Transfer Efficiency Increases

So We Can Increases The Mass Flow Rate And Velocity As It Increases It Will Increase The

Reynolds Number So For That We Have Calculated Reynolds Number At Mass Flow Rate Of

5 Kg/S.

Graph No.10 Reynold's No. Vs. Pressure Drop (Pa)

0

0.0005

0.001

0.0015

0.002

0.0025

0.003

0.0035

0.004

0 100000 200000 300000 400000 500000 600000 700000 800000 900000

Fri

ctio

n F

act

or

Reynold's No.

Reynold's No. Vs. Friction Factor

0

2000

4000

6000

8000

10000

12000

14000

0 100000 200000 300000 400000 500000 600000 700000 800000 900000

Pre

ssu

re D

rop

(P

a)

Reynold's No.

Reynold's No. Vs. Presure Drop (Pa)



There Are Multiple Factors Which Is Affected By A Single Parameter So We Cannot

Increase Or Decrease The Value Of Any Parameter Because Other Parameter Are Also

Connected To That Same Value As We Have Seen Above The Increase In Reynolds Number

Will Reduce The Pressure Drop But At The Same Time If The Reynolds Number Increases The

Pressure Drop Will Also Increases So It Is Advisable That Pressure Drop Should Not Be

Increased Very Much And Every Parameter Are Balanced Properly.

3.3 Calculation For Heat Exchanger 2

Data:

o Pipe Inner Diameter: 0.05m

o Pipe Outer Diameter: 0.058m

o Hot Water Outlet From Heat Exchanger – 1 : 95℃

o Hot Water Inlet To Heat Exchanger - 2 : 40℃

o Heat Supplied From Heat Exchanger : 553.212 Kw

o No. Of Tanks To Be Heated Required : 5

o Heat Required For Each Tank : 110.6524 Kw

o Mass Flow Rate Of Hot Water From Heat Exchanger : 2.4 Kg/S



Chapter-4 Modelling And Simulation

4.1 Rough Model For Conceptualization & Imagination

Figure No.4 Rough Model For Imagination

For The Understanding Of The Design And Its Surrounding Environment The Rough

Model Has Been Prepared By Us In Which We Have Prepared A Scale Model Of Gas

Furnace And The Chemical Line Passing Near The Furnace. We Also Have Design The

Exhaust Same As The Current Plant, But The Things Are Modified As We Have To Design

And Utilize That Exhaust Heat Of The Flue Gases.

At The Same Time We Have Also Done The Assembly Of The Additional Equipment

Used For The Project Like Distribution Piping Line, Heat Exchanger-1, Heat Exchanger-2,

And Its Coupling. This Will Work In Visualization Of The Design And With The Help Of

This We Can Easily Identify The Theoretical Design Dimension Are Possible Or Not.

The Model Is Also Near To The Original Scale So The Spacing Between The Furnace

And The Tank Is One Of The Critical Parameter For Design And Installation. Thus With

This Model We Can Easily Identify Whether The Design Is Feasible Or Not.



4.2 Modelling & Assembly In Software

Figure No.5 Modelling Of Heat Exchanger-1

As We Have Calculated The Pipe Length And All Other Parameter Theoretically Then We

Started Modelling The Heat Exchanger – 1 As Per The Dimension Of The Theoretical

Calculation So We Started Making The Part File In Solidworks And Then After We Have

Assembled It. The Above Fig Is F Heat Exchanger – 1 Which Is A Tube In Tube Type Heat

Exchanger.

In This We Will Supply The Hot Flue Gases From The Large Section Of Pipe And

Simultaneously Cold Water Will Flow In Small Section Of Pipe Both The Flow Are In Counter

To Each Other So The Overall L.M.T.D. Is More Which Will Increase The Heat Transfer Rate.

Figure No.6 Sectional View Of Heat Exchanger-1



This Is The Sectional View Of The Above Model Of Heat Exchanger – 1 Which Shows

The Inner Sectional Side Of The Pipes This Gives A Brief View Of The Inner Side Of The

Pipe.

4.3 Meshing Of Heat Exchanger-1

Figure No.7 Fine Meshing Of Heat Exchanger – 1 In Ansys

Once The Modelling And Assembly Is Done The Modelling File Is Saved As Part Or

Assembly File Then After It Is Also Saved As The .Stp Or In .Igs Format For Analysis Purpose.

Then After We Have Done Our Analysis In Ansys Multi-Physics Which Gives Us The Wide

Range Of Analysis Platform, In That There Are Many Modules Of Analysis But As We Are

Dealing With Fluid As Well As The Temperature We Have Selected The Cfd(Fluent) Analysis

Module Which Gives The Flow As Well As The Temperature Distribution, Pressure Drop

Results.

In That We Have To Fill The Hollow Section By Capping The Surface And Making It A

Solid Section Which Act As A Fluid In The Pipe. So Both Of The Section Is To Be Filled By

The Different Capping And After That Name Section Is Provided To Each Of The Surface Of

The Model Which Will Be Useful At The Time Of Giving Boundary Condition. Once All This

Procedure Is Done We Have To Update The Module Then After We Have To Define Meshing

To Whole Body The Meshing Is First Done With Simple Predefined Selection, After Seeing The

Result Of The General Mesh We Will Optimize The Meshing And Make The Selection Very

Fine To Have More Accurate Answers, We Also Cross Check The Meshing By Different

Meshing Statistics Technique Like Aspect Ratio, Jacobean Ratio, Warping Factor, Skewness

Methods. Out Of All This Methods The Meshing Results Must Come Under The Boundary Of

Any Three Methods.



4.4 Analysis & Simulation Of Heat Exchanger-1

As The Meshing Is Completed We Have To Run The Setup Module In This We Have To

Apply Different Boundary Conditions As We Want To Have The Real Time Situation Answer

We Have To Apply All The Parameter Acting On It That Is Gravity Which Is 9.81 M/S. As The

Flow Is Turbulent We Have To Select The Factor On Which The Turbulent Flow Is Working In

This Analysis We Have Taken The K- Epsilon. Then After We Have To Provide The Material

To The Section That Is Solid To The Tank And Pipeline And Liquid And Gas To The Fluid.

There After The Boundary Condition As Per The Requirement Of The Model. Then Initialize It

And Run The Number Of Iterations More The Iteration Good The Answer.

Figure No.8 Temperature Distribution In Water (Working Fluid)

As We Have Defined The Parameter As Per The Above Description Then The

Computational Work Will Start Solving The Iteration And After Few Time We Will Get The

Results Of The Module. In This Above Image We Can See The Colour Difference In The Pipe

Which Indicate That The Change In Temperature Take Place As The Flue Gases Pass The Heat

To The Cold Water It Will Start Heating The Water And The Exhaust Flue Gases Will Loses Its

Temperature So Due To This We Can See This Type Of Image.



Figure No.9 Stream Line With Water Particle At Different Temperature

Base On That Flow We Can Create The Stream Line And See How Actually The Inner

Pipe Fluid Will Flow And This Fig Shows The Result Of That Simultaneously We Can Also See

How Water Particles Gain The Heat And Flow Through Pipe.

4.5 Modelling & Assembly Of Heat Exchanger-2

Figure No.10 Model Of Heat Exchanger – 2

As We Have Calculated The Pipe Length And All Other Parameter Theoretically Then We

Started Modelling The Heat Exchanger – 2 As Per The Dimension Of The Theoretical

Calculation So We Started Making The Part File In Solidworks And Then After We Have



Assembled It. The Above Fig Is F Heat Exchanger – 2 Which Is A Tube In Tube Type Heat

Exchanger.

In This We Will Supply The Hot Water Generated By The Heat Exchanger – 1, The U

Shape Pipe Will Carry That Hot Fluid And Flow From The Upper Side To Lower Side, Outside

The Small Pipe The Chemical Is Filled In Tank Which Is To Be Heated The Tank Contain 85%

Of Water And Remaining 15 % Chemical Mixture Thus We Have Taken The Heat Transfer

Coefficient Of Water As The Tank Contain Maximum Portion Of It.

The Hot Water Passes Stage By Stage In Tank And Supply Heat To Tank Chemical The

Chemical Temperature Will Rise And The Water Temperature Will Drop Down As It Will Be

Cooled Down The Naturally Its Density Will Increases And It Will Move In Down Direction, So

At The Bottom Part We Will Collect The Cold Fluid And Again Send It To The Heat Exchanger

– 1, After A Certain Period Of Time The Chemical Temperature Raises As Per The Required

Level.

Figure No.11 Sectional View Of Heat Exchanger – 2

This Is The Sectional View Of The Above Model Of Heat Exchanger – 1 Which Shows

The Inner Sectional Side Of The Pipes This Gives A Brief View Of The Inner Side Of The Pipe.

As In The Sectional View We Can Easily See That The Pipe Is Distributed In Whole Tank So It

Will Cover Up The Overall Tank Fluid And Heat Up The Chemical From All Direction Evenly

This Will Reduce The Heating Tie Of Chemical So We Can Achieve Our Desired Temperature

In Lesser Time, Which Will Be More Useful At The Time Of Production.

Once The Modelling And Assembly Is Done The Modelling File Is Saved As Part Or

Assembly File Then After It Is Also Saved As The .Stp Or In .Igs Format For Analysis Purpose.

Then After We Have Done Our Analysis In Ansys Multi-Physics Which Gives Us The Wide

Range Of Analysis Platform, In That There Are Many Modules Of Analysis But As We Are

Dealing With Fluid As Well As The Temperature We Have Selected The Cfd(Fluent) Analysis

Module Which Gives The Flow As Well As The Temperature Distribution, Pressure Drop

Results.



In That We Have To Fill The Hollow Section By Capping The Surface And Making It A

Solid Section Which Act As A Fluid In The Pipe. So Both Of The Section Is To Be Filled By

The Different Capping And After That Name Section Is Provided To Each Of The Surface Of

The Model Which Will Be Useful At The Time Of Giving Boundary Condition.

4.6 Meshing Of Heat Exchanger-2

Once All This Procedure Is Done We Have To Update The Module Then After We Have To

Define Meshing To Whole Body The Meshing Is First Done With Simple Predefined Selection,

After Seeing The Result Of The General Mesh We Will Optimize The Meshing And Make The

Selection Very Fine To Have More Accurate Answers, We Also Cross Check The Meshing By

Different Meshing Statistics Technique Like Aspect Ratio, Jacobean Ratio, Warping Factor,

Skewness Methods. Out Of All This Methods The Meshing Results Must Come Under The

Boundary Of Any Three Methods.

Figure No.12 Fine Meshing Of Heat Exchanger – 2



4.7 Analysis & Simulation Of Heat Exchanger-2

As The Meshing Is Completed We Have To Run The Setup Module In This We Have To Apply

Different Boundary Conditions As We Want To Have The Real Time Situation Answer We Have

To Apply All The Parameter Acting On It That Is Gravity Which Is 9.81 M/S. As The Flow Is

Turbulent We Have To Select The Factor On Which The Turbulent Flow Is Working In This

Analysis We Have Taken The K- Epsilon. Then After We Have To Provide The Material To The

Section That Is Solid To The Tank And Pipeline And Liquid And Gas To The Fluid. There After

The Boundary Condition As Per The Requirement Of The Model. Then Initialize It And Run

The Number Of Iterations More The Iteration Good The Answer

Figure No.13 Temperature Distribution In Chemical



Chapter-5 Canvas Activity

5.1 Aeiou Canvas

The Aeiou Stands For Activity, Environment, Interaction, Objective And Users. In This Canvas

All The Above Activities Are Included As Per The Project Aspect. This Canvas Is Helps Us To

Make Our Project Plan Clear And Use To Develop The Path For The Project.

Activities

This Category Is Use To Make Our Future Activities Clear And Also Generate

The Path And Flow Process So One Can Easily Get What To Do First.

Environment

The Nearby Area Surrounded By The Site Is Considered In The Environment As

We Are Working With High Temperature The Environment We Have Higher

Temperature.

Interaction

Each And Every Person Connected To This Project Comes Under This Word.

Start With H.R.People And Administrative And Then General Manager, Plant

Head, Supervisor, Operator, Worker.

And From College Internal Guide And Other Faculty Have Supported In This

Project Work.

Objective

The Main Objective Of Our Project Is To Utilize The Exhaust Flue Gas

Temperature To Heat Up The Nearby Phosphating Line. This Will Decrease The

Plant Energy Cost And Thus The Plant Efficiency Increases In Terms Of Energy

As The Company Is Using Energy Conservation To Eco-Friendly Plant The

Company Also Get Iso Standardization Which Create Good Market Value.

As The System Is Simple And Easy In Construction The Maintenance Is Very

Less Compare To Current Plant.

Users

The Key User Is Company Itself, And Its Employees.

The Stakeholder And The Other Vendor Are Also Part Of This User Indirectly.



Figure No.14 Aeiou Canvas



5.2 Empathy Canvas

This Canvas Is Based On To Show Our Project How Is Defined & To Present To Industrial Shodh

Yatra (Isy). The Objective Is To Adopt Systematic Approach Based On Design Thinking And

Articulate The Insights Derived From Empathization Process Including Observation, Interaction

Etc. During Isy (Industrial Shodh Yatra) And Finalise The Problem/Idp/Udp Definition And

Orient The Task As Their Final Year Project In Their 7th And 8th Semester.

Observation

In Observation Box We Put Notes & Bullets Of Our Idp Project In Which We

Include The Different Shops & Places Of Industries.

Our Project Is Based On Our Summer Internship In Echjay Industries Pvt. Ltd.

Scouted Challenges

In Scouted Challenges We Include The Challenges Or Problems Which Is

Facing By Industry.

In Canvas By Use Of Sticky Notes We Shows Many Challenges And

Problems Which We Shows In Our Summer Internship In Industry.

Top Five Problems On The Basis Of Desirability, Feasibility & Viability

In This Section We Define Top Problems For Our Final Year Project Which

Can Completed By Us In One Year.

We Define The Project On The Different Sectors Like Thermal, Material

Handling, And Manufacturing & Energy Conservation.

Final Problem

After Defining Top 5 Problems In Industry, We Focused On Main Problem

Which Is Basis On Thermal & Energy Conservation. Which Is “Design Of

Heat Exchanger For Waste Heat Utilization From Exhaust Gases Of

Furnace.”



Figure No.15 Empathy Canvas



5.3 Ideation Canvas

5.3.1 Ideation Canvas

To Adopt A Systematic Design Thinking Approach To Ideate And Approach Towards Solving

The Defined Challenge, Finalized In Canvas Exercise 1. This Effort Will Bring In Various

Heuristics For Solving A Challenge Using Multiple Ways.

The Team Needs To Pick Up The Best Optimized Path From The Whole Ideation Output

And Proceed For Product/Solution Design.

In This Canvas We Focused On This Project In Socially, Place & Related Activities.

o People

o In This Section We Mentioned The People Which Are Directly & Indirectly Is

Connected With This Project.

Our Project Is Related To Industry So Many Peoples, Stakeholders Are Connected

And These Project Is Inflected With Them.

o Activities

In This Section We Mentioned The Activities Which Is Going To Take In This

Project Which Are:

Literature Survey

Data Collection

Theoretical Design

Computational Design

Analysis

Material Availability

Optimization

Demo Model

o Situation/ Context / Location

In This Section We Mentioned The Parameters, Dimensions, Area Constraints

Which Is Inflected To The Project.

Some Of Are:

Annealing Oil Fire Furnace

Phosphating Plant

Material Crane

Material Tray

Human Ergonomics

Tank Size

Temperature Regulations



o Possible Solutions

In This Section We Mention Which Solution & Results Can Be Achieved By Us

During Project Phase.

Figure No.16 Ideation Canvas



5.3.2 Ideation Funnel Canvas

Ideation Funnel Canvas Is Interconnected To Ideation Canvas But In The Detailed Way. In

This Canvas We Are Mainly Focused On The People, Activities And Problems.

o People

In This Section We Mentioned The People Which Are Mostly Connected

With This Project.

Our Project Is Related To Industry So Many Peoples, Stakeholders Are

Connected And These Project Is Inflected With Them.

o Activities

In This Section We Mentioned The Activities Which Is Going To Take In

This Project.

In This Canvas We Mentioned The Activity In Which Are Currently

Working On. Which Are :

Literature Survey

Data Collection

Theoretical Design

o Problems

In This Part We Mentioned The Few Parameters & Constraints Which We

Have To Deal With It.

Temperature And Water Flow Control

Area Constraints

Multiple Solutions In Theoretical Calculations

o Situation/ Context / Location

In This Section We Mentioned The Parameters, Dimensions, Area

Constraints Which Is Inflected To The Project.

Some Of Are:

Annealing Oil Fire Furnace

Phosphating Plant

Human Ergonomics



o Possible Solution

In This Section We Mention Which Solution & Results Can Be Achieved

By Us During Project Phase.

In Which We Are Directly Focusing On.

o Inputs

In This Section We Mentioned The Inputs Which Is Given By Us To This

Project By Which We Can Achieve Our Main Target.

Theoretical Calculations

o Mechanical Inputs

o Thermal Inputs

o Fluid-Flow Inputs

o Mathematical Equations

Figure No.17 Idea Funnel Canvas



5.4 Product Development Canvas

This Exercise Is Meant For Giving Strategic Orientation To The Project Of Each Team So That

It Achieves Its True Goal As Defined By The Previous Canvas Exercises. This Exercise Is More

About Developing Strategy For The Proposed Product/Solution Design, After The Team Has

Successfully Attempted The Ideation Process And Has Incorporated Inputs From All

Stakeholders.

o Purposes

In This Section We Mentioned The Purposes, Our Main Goal Of This

Project. In This Section We Mentions The Advantages Of This Project To

The Industry And Our Perspective. Which Are:

Waste Heat Utilization

Energy Conservation

Plant Efficiency Improvement

Overall Cost Reduction

ISO Environmental Standardization

Market Value.

o Product Function

In These Part We Mentioned The Product Function Of Our Components

Which Is Going To Be Part Of This Project.

o Product Features

In This Section We Mentioned The Features Of Our Components Which

Enhance The Value Of Our Project.

Compact Design

Temperature Sensors And Valve Controller

Effective Heat Transfer Material

Sensitive System

o Customer Revalidation

In These Section We Put Three Factors In Which Our Product Is Deal

With Our Customers.

Cost

Product Life Cycle

Problem In Generating Required Output

o Reject/Redesign/Retain

We Mentioned Over Here Factors Of Redesign If The Customers Are Not

Satisfying With Our Product.

Raw Material Change



Redesigning Heat Exchanger By Providing Fin.

Figure No.18 Production Development Canvas



5.5 Business Canvas

Key Partners

This Are Few Of The Reputed Companies Working With Echjay

Industries Pvt. Ltd. Companies Like Larson And Toubro, Mahindra,

Cat, Godrej, Siap, Tafe, Bmw, Audi. Etc. As We Develop The Echjay

Plant We Can Also Encourage The Partner Company To Get The

Advantage Of The Production Technology.

Key Activities

The Company Is Mainly Based On Forging Which Contain Cold

Forging Having Capacity Of 2500 Kn Fully Automatic Four Stage

Forging Machine. The Company Also Have Hot Rolling Line (HRL),

Axial Closed Die Rolling (ACDR), Ring Rolling, And It Also Have

High-Tech Machine Shops Equipped With CNC VMC And Automatic

Robots.

Key Resources

The Company Is Highly Managed And Have Good Chain Of Upward

And Downward Communication Chain Which Lead To A Clear

Message To Each And Every Employee Of The Company Having

Good Executive And Hr Staff, General Manager, Design Team,

Maintenance Team, Production Manager, Supervisor, Worker,

Helpers. Which Provide Company A Good Structure.

Value Propositions

The Company Is Serving With Good Products So The Quality Of The

Product Will Definitely Be Good, As Quality Is Good And The

Company Is Following Many Standardization The Life Span Of The

Product Will Be Good.

Customer Relationship

Company Is Highly Ethical To The Customer Point Of View This

Itself Says That Company Is Maintaining A Very Good Image To The

Customer.

Customer Segments

80% Of The Company Production Is Of Automotive Segment, 15%

Of The Part Is Of Heavy Duty Piping And Refining Industries,

Remaining 5% Of The Products Are Heavy Duty Marine And

Aerospace Application

Channels

The Company Have A Good Media Advertising In Different Medium

Like Facebook, Twitter, LinkedIn, YouTube, Just Dial, Yellow Pages.



Cost Structure

The Main Cost Of The Plant Is The Running Cost, Then After The

Maintenance Cost, The Cost In Research And Development And

Promotional Events And Charity

Revenues Streams

The Project Will Help To Reduce The Production Cost This Will Lead

To Profit Increase The Advantage Is That Environmental Pollution

Will Also Be Reduced So The Company Can Have Iso Certification.

As The Design Is Simple The Maintenance Cost Will Also Be

Reduced So After Some Time We Can Easily Achieve The Payback

Period Of The Installation Product Which Lead To Net Increment In

Profit.



Figure No.19 Business Canvas



Chapter-6 Results And Future Working Plan

6.1 Result And Conclusion

By This Theoretical Calculation We Got The Length Of Our 1st Heat Exchanger Which Is

25m. And On Basis Of That We Are Calculating The Remaining Few Parameter By This

Procedure We Have Define Many Different Possible Way To Find The Results.

We Have Find The Optimized Dimensions For Heat Exchanger-1 & Heat Exchanger-

2 With Respect To Available Heat From Exhaust Gas.

From This Research About Exchanger We Have Observed That By Changing The

Mass Flow Rate Of Hot Fluid Liquid, The Effective Heat Transfer Area Will

Decrease.

But Also The Pumping Work & Pressure Drop Increases Which Create More Energy

Consumption.

Table No.9 Changing In Pipe Lengths With Respect To Changes In Mass Flow Rate & Pipe

Material (Id 50mm & Od 58mm)

Mass Flow Rate (Hot

Fluid) 3 4 5 6 7 8 9

201 Annealed Steel Ss

(K=19.841 W/M.K)

49.171

8

33.194

7

26.1509

5

22.04

8

19.3

2

17.3

7 15.89

AISI 1015, Cold Drawn

Ss (K=52 W/M.K) 47.63 31.93 25 20.95

18.2

7

16.3

4 14.888

AISI 304 (K = 16.3

W/M.K) 55.78 41.018 26.55

22.43

1

19.6

9

18.1

8

16.247

7

AISI 4130 Steel ( K=42.7

W/M.K) 47.84 32.105 25.155

21.10

8

18.4

1

16.4

8 15.023

Copper (K=345 W/M.K) 46.82 31.27 24.39 20.39

17.7

2 15.8 14.36

Aluminium (K= 234

W/M.K) 46.88 31.32 24.42 20.43

17.7

6

15.8

5 14.4



Graph No.11 Heat Transfer Pipe Length Vs. Mass Flow Rate With Respect To Different

Material

From This Graph We Observed That There Is Less Difference Between Pipe Lengths

With Respect To Material From Higher Thermal Conductive To Lower Thermal

Conductive.

Copper Is The High Thermal Conductive Material In All Of This Materials, So It Gives

High Transfer Rate For Heat Exchanger, But As Per Market Value Copper Is Costlier

Material In All Of This Material We Have Selected.

0

10

20

30

40

50

60

0 1 2 3 4 5 6 7 8 9 10

Hea

t T

ran

sfer

Pip

e L

ength

m

Mass flow rate (Hot Fluid) Kg/s

Mass flow rate (Hot Fluid) Kg/s Vs. Heat transfer pipe m

201 Anneled Steel SS (K=19.841 W/m.K)

Aisi 1015, Cold Drawn SS (K=52 W/m.K) AISI 304 (K = 16.3 W/m.K)

AISI 4130 Steel ( K=42.7 W/m.K) Copper (K=345 W/m.K)

Aluminium (K= 234 W/m.K)



As Per Guidance Of Our Industrial Guide industry would recommend to use stainless

steel which is cheaper than copper & it’s maintainace cost is low.

After This Research We Can Determine The Dimensions Of Heat Exchanger-1.

1. Inner Pipe Diameter (Water) :- 50 Mm

2. Outer Pipe Diameter (Water) :- 58mm

3. Inner Pipe Diameter (Hot Air) :- 58mm

4. Outer Pipe Diameter (Hot Air) :- 470 Mm

5. Hot Fluid Inlet Temperature :- 300℃

6. Hot Fluid Outlet Temperature :- 191.633℃

7. Cold Fluid Inlet Temperature :- 40℃

8. Cold Fluid Outlet Temperature :- 90℃

9. Hot Fluid Mass Flow Rate :- 5 Kg/S

10. Cold Fluid Mass Flow Rate :- 2.4 Kg/S

11. Heat Exchanger-1 Length (No. Of Pass=1, Id=50mm, Od=58mm,

Material=Copper) :- 24.39813036 Meter

12. Logamathric Mean Temperature Difference :- 176.9758109℃

13. Generated Pressure Drop (In Hot Fluid) :- 6344.589 Pa

14. Generated Pressure Drop (In Cold Fluid) :- 12539.989 Pa

15. Required Pumping Work (In Hot Fluid) :- 48218.5 W

16. Required Pumping Work (In Cold Fluid) :- 38.3837 W

Future Working Plans:-

Theoretical Design Calculation For Heat Exchanger -2

Optimization Of Heat Exchanger-2

Application Of Heat Transfer Fin To Increase Heat Effectiveness

Butterfly Valve Control System To Control The Flow Rate Of Hot Flue Gases

Coming From The Furnace.

Use Of Baffle Plates To Increase The Heat Transfer Process.

Break Event Point Calculation For This Project.



Appendix-1

Air Properties At Atmospheric Pressure As A Function Of Temperature

Temperature Conductivity Cp Prandlt’s Density Viscosity

[K] [W/M.K] [Kj/Kg.K] Number [Kg/M3] [N·S/M2]

200 0.0181 1.007 0.737 1.7458 0.00001325

250 0.0223 1.006 0.72 1.3947 0.00001596

300 0.0263 1.007 0.707 1.1614 0.00001846

350 0.03 1.009 0.7 0.995 0.00002082

400 0.0338 1.014 0.69 0.8711 0.00002301

450 0.0373 1.021 0.686 0.774 0.00002507

500 0.0407 1.03 0.684 0.6964 0.00002701

550 0.0439 1.04 0.683 0.6329 0.00002884

600 0.0469 1.051 0.685 0.5804 0.00003058

650 0.0497 1.063 0.69 0.5356 0.00003225

700 0.0524 1.075 0.695 0.4975 0.00003388

750 0.0549 1.087 0.702 0.4643 0.00003546

800 0.0573 1.099 0.709 0.4354 0.00003698

850 0.0596 1.11 0.716 0.4097 0.00003843

900 0.062 1.121 0.72 0.3868 0.00003981

950 0.0643 1.131 0.723 0.3666 0.00004113

1000 0.0667 1.141 0.726 0.3482 0.00004244



Appendix-2



Appendix-3

Saturated Water Properties

Temperature Conductivity Cp Hfg Prandlt’s Viscosity Vap. Sp.

Vol.

Liq. Sp.

Vol.

[K] [W/M.K] [Kj/Kg.K] [Kj/Kg] Number [N·S/M2] [M3/Kg] [M3/Kg]

273.15 0.569 4.217 2502 12.99 0.00175 206.3 0.001

275 0.574 4.211 2497 12.22 0.00165 181.7 0.001

280 0.582 4.198 2485 10.26 0.00142 130.4 0.001

285 0.590 4.189 2473 8.81 0.00123 99.4 0.001

290 0.598 4.184 2461 7.56 0.00108 69.7 0.001001

295 0.606 4.181 2449 6.62 0.00096 51.94 0.001002

300 0.613 4.179 2438 5.83 0.00086 39.13 0.001003

305 0.620 4.178 2426 5.20 0.00077 29.74 0.001005

310 0.628 4.178 2414 4.62 0.00070 22.93 0.001007

315 0.634 4.179 2402 4.16 0.00063 17.82 0.001009

320 0.640 4.180 2390 3.77 0.00058 13.98 0.001011

325 0.645 4.182 2378 3.42 0.00053 11.06 0.001013

330 0.650 4.184 2366 3.15 0.00049 8.82 0.001016

335 0.656 4.186 2354 2.88 0.00045 7.09 0.001018

340 0.660 4.188 2342 2.66 0.00042 5.74 0.001021

345 0.668 4.191 2329 2.45 0.00039 4.683 0.001024

350 0.668 4.195 2317 2.29 0.00037 3.846 0.001027

355 0.671 4.199 2304 2.14 0.00034 3.18 0.00103

360 0.674 4.203 2291 2.02 0.00032 2.645 0.001034

365 0.677 4.209 2278 1.91 0.00031 2.212 0.001038

370 0.679 4.214 2265 1.80 0.00029 1.861 0.001041

373.15 0.680 4.217 2257 1.76 0.00028 1.679 0.001044

375 0.681 4.220 2252 1.70 0.00027 1.574 0.001045

380 0.683 4.226 2239 1.61 0.00026 1.337 0.001049

385 0.685 4.232 2225 1.53 0.00025 1.142 0.001053

390 0.686 4.239 2212 1.47 0.00024 0.98 0.001058

400 0.688 4.256 2183 1.34 0.00022 0.731 0.001067

410 0.688 4.278 2153 1.24 0.00020 0.553 0.001077

420 0.688 4.302 2123 1.16 0.00019 0.425 0.001088

430 0.685 4.331 2091 1.09 0.00017 0.331 0.001099

440 0.682 4.360 2059 1.04 0.00016 0.261 0.00111

450 0.678 4.400 2024 0.99 0.00015 0.208 0.001123

460 0.673 4.440 1989 0.95 0.00014 0.167 0.001137

470 0.667 4.480 1951 0.92 0.00014 0.136 0.001152

480 0.660 4.530 1912 0.89 0.00013 0.111 0.001167

490 0.651 4.590 1870 0.87 0.00012 0.0922 0.001184

500 0.642 4.660 1825 0.86 0.00012 0.0766 0.001203



References

1. Donald Q. Kern, "Process Heat Transfer Hardcover ", 1 Nov 1950

2. Holman J P , "Heat Transfer (In Si Units) (Sie)" ,Tata Mcgraw Hill Education Private

Limited-Paperback Edition-9th Edition

3. Sadik Kakaç, Hongtan Liu, Anchasa Pramuanjaroenkij "Heat Exchangers: Selection,

Rating, And Thermal Design, Second Edition

4. "Ramesh K. Shah (Author), Dusan P. Sekulic (Author) "Fundamentals Of Heat

Exchanger Design: Hardcover" , 15 Aug 2003

5. Yunus A. Cengel , "Heat & Mass Transfer: A Practical Approach”

6. United States Patent (10) Patent N0.: Us 6,626,235 B1 Christie (45) Date Of Patent:

Sep. 30, 2003

7. United States Patent Wang Et A]. Patent N0.:Us008540011b2

Us 8,540,011 B2 Date Of Patent: Sep. 24, 2013

8. United States Patent (12) (10) Patent N0.: Us 6,349,761 B1

(45) Date Of Patent: Feb. 26, 2002

9. United States Patent :- Us 2010/0175864a1 , Date Of Patent : Jul. 15, 2010

10. United States Patent: - Us 4328862a, Publication Date: Feb. 12, 1979.

11. United States Patent: - Us 20100175864a1, Application No: Us 11/917,994.

12. United States Patent: - Us 4858681a, Application No: Us 07/273,105, Publication

Date: Nov. 16, 1988.

13. United States Patent: - Us 5005637a, Application No: Us 06/727,345, Publication

Date: Nov. 5, 1986.

14. United States Patent: - Us 6568209 B1, Application No: Us 10/235,713, Publication

Date: Sep. 6, 2002.


Date: Sep. 12, 2002.


Date: Apr. 21, 2010.



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Remarks

Documents

IDP PROJECT REPORT