Faculty of Engineering
Department of Chemical Engineering
Cape Town Campus
CHEMICAL ENGINEERING TECHNOLOGY IV (Module 3)
(CET401S)
Heat Exchanger Design Assignment
Name & Surname
Student Number
Sharon Chakawa
214026523
Lecturer: Dr B. Godongwana
I certify that this is my own unaided work, except for the assistance received from the teaching
staff. I undertake not to pass this assignment onto any other student.
Signature (student): ………………………………............................ Date: 15/06/2017
Assessment criteria
%
Abstract
Introduction
Literature Review
Procedure
Results and Discussion
Conclusion & Recommendation
5
5
15
10
50
5
References
5
General Report Presentation
TOTAL:
5
100
Mark
Table of Contents
Abstract ..............................................................................................Ошибка! Закладка не определена.
List of Figures ............................................................................................................................................. ii
List of Tables ............................................................................................................................................... ii
Nomenclature.............................................................................................................................................. ii
1.
2.
Introduction.......................................................................................................................................... 1
1.1.
Background ................................................................................................................................. 1
1.2.
Aims and objective ..................................................................................................................... 1
Literature Review ............................................................................................................................... 2
2.1.
Shell and Tube Exchanger ....................................................................................................... 3
2.2.
Design Consideration ................................................................................................................ 4
i
2.2.1.
All Heat Exchanger Types ................................................................................................ 4
2.2.2.
Shell and Tube Exchangers.............................................................................................. 5
3.
Design Methodology .......................................................................................................................... 7
4.
Results and Discussion ..................................................................................................................... 7
5.
Conclusion ......................................................................................................................................... 15
6.
References ........................................................................................................................................ 16
7.
Appendix ............................................................................................................................................ 17
7.1.
Appendix A (Charts, (Sinnott, 2005)) .................................................................................... 17
Appendix B (Tables of constants, (Sinnott, 2005)) ......................................................................... 20
Table of Figures
Figure 1: parallel flow, counter flow and cross flow in a heat exchanger respectively (Rodriguez 1997) .....2
Figure 2: Temperature Profile of Two Fluid vs Heat Transfer (Kuppan, 2013). ................................................5
Figure 3: Plot of effectiveness of heat exchanger VS. Temperature fluid ..........................................................9
Figure 4: Plot of heat transfer area of heat exchanger VS. Outlet Temperature fluid .....................................9
Figure 5: Temperature correction factor: one shell pass; two or more even tube passes .............................17
Figure 6: Shell-bundle clearance .................................................................................................................................18
Figure 7: Shell-side heat-transfer factors, segmental baffles ......................................................................................19
Figure 8: Tube-side heat-transfer factor......................................................................................................................19
List of Tables
Table 1: Determination of Number of Tube Passes Based on Shell ID (Sinnott, 2005) .................................6
Table 2: Approximate values of overall heat-transfer coefficients ....................................................................20
Table 3: Constants for use in question 11 .............................................................................................................20
Table 4: Conductivity of metals ...............................................................................................................................21
Table 5: Fouling factors (coefficients), typical values ..........................................................................................21
Nomenclature
A
Th1
At
Th2
As
Uo
Vo
Cph
Cpc
heat transfer area (m2)
Inlet temperature of hot fluid (⁰C)
heat transfer area for tube side (m2)
Outlet temperature of hot fluid (⁰C)
Area for shell side (m2)
Overall heat transfer coefficient (W/m2∙⁰C)
Velocity of fluid (m / s)
Specific heat of hot fluid (kJ / kg∙K)
Specific heat of cold fluid (kJ / kg ∙K)
ii
De
Equivalent diameter (mm)
Di
Inner diameter of tube (mm)
Do
Outer diameter of tube (mm)
Db
bundle diameter (mm)
Dho
Header outer diameter (mm)
ds
Channel space (mm)
Di
Inner diameter of shell (mm)
F
Fouling Factor
G
mass velocity
L
Length of shell (m)
mh
Mass flow rate of the hot fluid (m / s)
mc
Mass flow rate of the cold fluid (m / s)
Dimensionless numbers
Nu
Nusselt number
Pr
Prandtl number
Re
Reynolds number
Jh
Heat transfer factor
Greek symbol
Δp
Pressure drop (pa)
Nt
Number of tubes
µ
Viscosity of fluid (kg /m∙s)
Pt
Tube pitch (mm)
ΔTlm
Log mean temperature different (⁰C)
Qc
Heat transfer rate of cold side (kW)
K
Thermal conductivity (W/ m ∙ ⁰C)
Qh
Heat transfer rate of hot side (kW)
ρ
Density of fluid (kg / m3)
Ro
Outer radius of spiral (mm)
h
Heat transfer coefficient (w/ m 2∙⁰C)
Tc1
Inlet temperature of cold fluid (⁰C)
Tc2
Outlet temperature of cold fluid (⁰C)
iii
1. Introduction
1.1.
Background
Heat exchanger is one of the most important processes in engineering. The purpose of a heat
exchanger is to transfer the heat between the flowing fluids. A heat exchanger is the process of
transferring heat from one fluid to another fluid.
A heat exchanger is a device that is used for the transfer of internal thermal energy between 2
or more fluids at different temperatures. In most heat exchangers the fluids are separated by a
heat transfer surface and ideally they do not mix.
1.2.
Aims and objective
The purpose of this project is to design a shell and heat exchanger with one pass and two tube
passes.
1
2. Literature Review
According to Shukla et al. (2015), a heat exchanger is a device that assists in the transfer of
heat from one fluid to another. In some cases, a solid wall may separate the fluids and prevent
them from mixing. However, in other designs, the fluids may be in direct contact with each other.
In the most efficient heat exchangers, the surface area of the wall between the fluids is
maximised while simultaneously minimizing the fluid flow resistance. Fins or corrugations are
sometimes used with the wall in order to increase the surface area and to induce turbulent flow.
In heat exchanger design, there are three types of flow arrangements, namely counter-flow,
parallel-flow, and cross-flow.
In the counter-flow heat exchanger, both fluids enter the
exchanger from opposite sides. While in the parallel-flow heat exchanger, the fluids come in
from the same end and move parallel to each other as they flow to the other side. Furthermore,
cross-flow heat exchanger moves the fluids in a perpendicular fashion. In comparison to the
other flow arrangements counter –flow is the most efficient design because it transfers the
greatest amount of heat (Widiawati, 2015).
Figure 1: parallel flow, counter flow and cross flow in a heat exchanger respectively
(Rodriguez 1997)
There are two major different designs of heat exchangers: shell and tube, and plate heat
exchanger. The most typical type of heat exchanger is the shell and tube design. This heat
exchanger can be designed with bare tube or finned tubes. One of the fluids runs through the
tubes while the other fluid runs over them, causing it to be heated or cooled. In the plate heat
exchanger, the fluid flows through baffles. This causes the fluids to be separated by plates with
a large surface area. This type of heat exchanger is typically more efficient than the shell and
tube design (Ravagnani et al., 2009).
2
2.1.
Shell and Tube Exchanger
Leong et al. (1998), describes a shell and tube heat exchanger as a class of heat exchanger
designs. It is the most common type of heat exchanger in oil refineries and other large chemical
processes, and is suitable for higher-pressure applications. It consists of a tube bundle enclosed
in a cylindrical casing called a shell. One fluid runs through the tubes, and another fluid flows
over the tubes through the shell to transfer heat between the two fluids.
Two fluids, of different starting temperatures, flow through the heat exchanger. One flows
through the tubes (the tube side) and the other flows outside the tubes but inside the shell (the
shell side). Heat is transferred from one fluid to the other through the tube walls, either from
tube side to shell side or vice versa. The fluids can be either liquids or gases on either the shell
or the tube side. In order to transfer heat efficiently, a large heat transfer area should be used,
so that there are many tubes. In this way, waste heat can be put to use. This is a great way to
conserve energy (Dixit et al., 2013).
Typically, the ends of each tube are connected to plenums through holes in tube sheets. The
tubes may be straight or bent in the shape of a U, called U-tubes. Most shell-and-tube heat
exchangers are 1, 2, or 4 pass designs on the tube side. This refers to the number of times the
fluid in the tubes passes through the fluid in the shell. In a single pass heat exchanger, the fluid
goes in one end of each tube and out through the other (Sinnott, 2005).
According to Selbas & Reppich (2006) , there are two basic types of shell-and-tube exchangers.
The first is the fixed tube sheet unit, in which both tube sheets are fastened to the shell and the
tube bundle is not removable. The second type of shell-and-tube unit has one restrained tube
sheet, called the stationary tube sheet, located at the channel end. Differential expansion
problems are avoided by use of a freely riding floating tube sheet at the other end or the use of
U tubes. This design may be used for single or multiple pass exchangers. The tube bundle is
removable from the channel end, for maintenance and mechanical cleaning.
There are often baffles directing flow through the shell side so the fluid does not take a short cut
through the shell side leaving ineffective low flow volumes (Kuppan, 2013).
Counter current heat exchangers are most efficient because they allow the highest log mean
temperature difference between the hot and cold streams. Many companies however do not use
single pass heat exchangers because they can break easily in addition to being more expensive
3
to build. Often multiple heat exchangers can be used to simulate the counter current flow of a
single large exchanger (Sinnott, 2005; Kuppan, 2013).
2.2.
Design Consideration
2.2.1. All Heat Exchanger Types
(a) Operating temperature
The operating temperatures of the exchanger are usually set by process conditions. However, in
certain cases, the exchanger designer will establish the operating temperatures. In a typical
refinery or petrochemical plant, exchangers may be operating at temperatures as high as
1000°F or as low as -200°F. These limits are dictated by material considerations, safety,
economics and ASME Code requirements.
(b) Effective temperature difference
The driving force for heat transfer is the “effective temperature difference," CMTD, between the
hot and cold fluids. This temperature difference is calculated from the counter-current log mean
temperature difference with a correction factor applied to account for the actual flow
arrangement (Kuppan, 2013).
Temperature approach
Sinnott (2005) defines temperature approach as the difference of the hot side and cold side fluid
temperatures at any point within a given exchanger. A temperature cross indicates a negative
driving force for heat transfer between the fluids. It requires either a large area for heat transfer
or high fluid velocities to increase the overall heat transfer coefficient. If outlet temperatures
form a cross in a multi-tube pass heat exchanger, a lower than desirable LMTD correction factor
will occur. A simple way to avoid this is to use more exchanger shells in series.
(c) Fouling factors
The increased resistance to both heat transfer and fluid flow caused by deposits on a heat
transfer surface is called fouling.
4
Fouling works as an insulating layer on the heat transfer surface, reducing heat transfer
efficiency (reduced duty) or decreasing available flow area (reduced throughput). The increased
resistance to heat transfer is represented by a quantity referred to as the fouling thermal
resistance, which is added to the total thermal resistance. The values of fouling thermal
resistance have generally been observed to increase with time. To account for the effect of
fouling on pressure drop requires an estimate of the fouling layer thickness (Shukla et al., 2015).
(d) Pressure drop
The pressure drop through a heat exchanger is made up of three losses: the frictional loss due
to flow, the losses due to changes in direction of flow and losses due to expansion and
contraction into and out of nozzles and tubes. In some exchangers, a change in the vertical
elevation of the fluid as it passes through the exchanger may cause a hydrostatic pressure loss
or gain (Widiawati, 2015).
2.2.2. Shell and Tube Exchangers
(a) Determination of number of shells based on graphical method as following
Figure 2: Temperature Profile of Two Fluid vs Heat Transfer (Kuppan, 2013).
(b) Tube Selection
According to Dixit et al. ( 2013), the following parameters are considered: material of tube,
Length , Diameter and wall thickness and Ferrules.
5
Table 1: Determination of Number of Tube Passes Based on Shell ID (Sinnott, 2005)
(c) Tube Site Flow
According to Sinnott (2005), whichever fluid appears higher on the following list will ordinarily
be passed through the tubes:
i.
Cooling water.
ii.
Corrosive fluid or a fluid likely to deposit coke, sediment or other solids.
iii.
Fouling fluid, which the fluid can cause fouling.
iv.
Fluid with the less viscosity.
v.
The fluid under higher pressure
vi.
The hotter fluid.
vii.
Less volume fluid.
(d) Fluid velocity
Liquid - Tube side: 3 – 7 ft/s and maximum is 13 ft/s if there is a need to reduce fouling; Water is
5 – 8 ft/s.
Shell side: 1 – 3 ft/s
Vapour – Vacuum: 164 – 230ft/s;
Atmospheric: 33 - 98ft/s;
High pressure: 16 – 33ft/s
(Sinnott 2005; Kuppan 2013)
6
3. Design Methodology
1. Define the duty: heat-transfer rate, fluid flow-rates, and temperatures.
2. Collect together the fluid physical properties required: density, viscosity, thermal
Conductivity.
3. Decide on the type of exchanger to be used.
4. Select a trial value for the overall coefficient, U.
5. Calculate the mean temperature difference, Tlm.
6. Calculate the area required.
4. Results and Discussion
Following data is adopted for design of a shell and tube heat exchanger which is described
below,
7
Inner temperature of shell side (Th1) : 100 °C
Inner temperature of tube side (Tc1) : 40 °C
Mass flow rate of Steam (ms): 1.08 kg/s
Assumed values
Tube outer diameter (do): 50.08 mm
Tube inner diameter (di): 43.99 mm
Pitch (pt): 1.25do
1. By using various exit temperatures, the effectiveness of a heat exchanger can be
determined (Holman, 2010).
Water will be used as the minimum flow.
𝐶𝑚𝑖𝑛 = 𝑚𝑤 𝐶𝑝𝑤
𝑞 = 𝐶𝑚𝑖𝑛 (𝑇𝑜 − 𝑇𝑖 )
𝑞
𝐶𝑚𝑖𝑛 =
(𝑇𝑜 − 𝑇𝑖 )
𝑁𝑇𝑈 (𝑁) =
𝐴𝑈
𝐶𝑚𝑖𝑛
𝑈 𝑖𝑠 𝑎𝑠𝑠𝑢𝑚𝑒𝑑 𝑡𝑜 𝑏𝑒 1500
𝑊
𝑚2 ∙ ℃
−
𝐴𝑈
𝜖 = 1 − 𝑒 −𝑁 = 1 − 𝑒 𝐶𝑚𝑖𝑛
According to Holman (2010), at equilibrium:
𝑞 = 𝜖𝐶𝑚𝑖𝑛 (𝑇𝑠 − 𝑇𝑖 )
−
𝐴𝑈
∴ 𝑞 = [1 − 𝑒 𝐶𝑚𝑖𝑛 ] 𝐶𝑚𝑖𝑛 (𝑇𝑠 − 𝑇𝑖 )
∴𝐴=
−𝐶𝑚𝑖𝑛
𝑞
ln [1 −
]
𝑈
𝐶𝑚𝑖𝑛 (𝑇𝑠 − 𝑇𝑖 )
By using polymath a plot of effectiveness and area of heat exchanger to outlet
temperature of fluid for 40 ℃ < 𝑇𝑂 < 100 ℃ is generated.
8
Figure 3: Plot of effectiveness of heat exchanger VS. Temperature fluid
Figure 4: Plot of heat transfer area of heat exchanger VS. Outlet Temperature fluid
9
By considering the effectiveness of heat exchanger, the outlet temperature of fluid is chosen as
75℃ .
𝑞 = 𝑚𝑠 ʎ𝑠 = 1.083 × 2257
= 2444.3 𝑘𝑊
2.
3. 𝑞 = 𝑚𝑐 𝐶 𝑝 (𝑇𝑐,𝑜𝑢𝑡 −𝑇𝑐 ,𝑖𝑛 )
𝑚𝑐 =
2444.3
4.184 (75 − 40)
= 16.69 𝑘𝑔/𝑠
4. Assume Counter- Current Flow
∴ ∆𝑇𝑙𝑚 =
(𝑇ℎ,𝑖𝑛 −𝑇𝑐,𝑜𝑢𝑡 ) − (𝑇ℎ,𝑜𝑢𝑡 −𝑇𝑐,𝑖𝑛 )
𝑇 −𝑇𝑐,𝑜𝑢𝑡
)
𝑇ℎ,𝑜𝑢𝑡 −𝑇𝑐 ,𝑖𝑛
ln ( ℎ,𝑖𝑛
∆𝑇𝑙𝑚 =
(100 − 75 ) − (100 − 60)
100 − 75
100 − 40 )
ln (
= 40 ℃
5. Based on the heat exchanger configuration the Temperature correction factor for 1 shell-2
tube pass exchanger is obtained from figure 5
𝑅=
𝑇1 − 𝑇2
𝑡2 − 𝑡1
𝑆=
𝑡2 − 𝑡1
75 − 40
=
= 0.583
𝑇1 − 𝑡1
100 − 40
=
100 − 100
=0
75 − 40
∴ 𝐹𝑡 = 1
7. The mean temperature difference is calculated using DTm  Ft  LMTD:
𝐷𝑇𝑚 = 1 × 40
= 40 ℃
8. Assume overall heat transfer coefficient as initial guess from table 2.
10
Therefore U = 1500 W/m2°C
9. Calculate the provisional area : 𝐴 =
𝑞
𝑈𝐷𝑇𝑚
2444.3 × 103
𝐴=
1500 × 40
= 40.74 𝑚2
10. Number tubes
𝑁𝑡 =
𝑁𝑡 =
𝐴
𝜋𝑑0 𝐿
40.74
𝜋 × 0.0508 × 3
𝑁𝑡 = 85.1 ≈ 86 𝑡𝑢𝑏𝑒𝑠
11. Tube pitch and the bundle diameter
𝑃𝑡 = 1.25 𝑑0
1
𝑁𝑡 𝑛1
𝐷𝑏 = 𝑑0 ( )
𝐾1
Where K1 and n1 are obtained from the table based on the type of tube arrangement (Triangular or
square pitch) in (table 3). K1 and n1 is 0.249 and 2.207 respectively
1
86 2.207
𝐷𝑏 = 0.0508 × (
)
0.249
= 0.7178𝑚
12. Assuming the type of floating head of the exchanger to be a split-ring floating head type.
The bundle diameter clearance, BDC is obtained from figure 6
∴ 𝐵𝑢𝑛𝑑𝑙𝑒 𝑑𝑖𝑎𝑚𝑒𝑡𝑟𝑖𝑐𝑎𝑙 𝑐𝑙𝑒𝑎𝑟𝑎𝑛𝑐𝑒 (𝐵𝐷𝐶) = 63 𝑚𝑚
13. shell diameter:
𝐷𝑠 = 𝐷𝑏 + 𝐵𝐷𝐶
𝐷𝑠 = 0.7178 + 0.063
𝐷𝑠 = 0.7808𝑚
11
14. Shell Side Coefficient
Baffle spacing :
𝐵𝑠 = 0.4 × 𝐷𝑠
= 0.4 × 0.7808
∴ 𝐵𝑠 = 0.31232 𝑚
Area for cross flowing
𝐴𝑠 =
=
(𝑃𝑡 − 𝑑𝑜 )𝐷𝑠 𝐵𝑠
𝑃𝑡
(0.0635 − 0.0254) × (0.7808)(0.312332)
0.0635
= 0.04877 𝑚2
Shell side mass velocity:
𝐺𝑠 =
16.69
= 22.21 𝑘𝑔/𝑠
0.04877
Shell equivalent Diameter:
1.10
(𝑃𝑡 2 − 0.917𝑑0 2 )
𝑑0
1.10
(0.06352 − 0.917(0.0508)2 )
=
0.0508
𝑑𝑒 =
= 0.0766 𝑚
Shell side’s Reynolds number
𝐺𝑠 𝑑𝑒
𝜇
22.21 × 0.0766
=
0.00001227
𝑅𝑒 =
= 138 654 (𝑇𝑢𝑟𝑏𝑢𝑙𝑒𝑛𝑡 𝑓𝑙𝑜𝑤)
Shell side transfer coefficient:
ℎ𝑜 𝑑𝑜
𝜇 0.14
= 𝑗ℎ 𝑅𝑒𝑃𝑟 0.33 ( )
𝑘𝑓
𝜇𝑤
𝜇
Neglect (𝜇 )
𝑤
Choose 25% baffle cut and jh is obtained from figure 7.
∴ 𝑗ℎ = 1.6 × 10−1
12
∴
ℎ𝑜 =
1
0.0251
× 0.16 × 138 654 × 13
0.0508
= 7269 𝑊/𝑚2 ∙ ℃
15. Tube - side coefficient
40 + 75
= 57.5℃
2
2
𝜋𝑑𝑖
0.043992
𝑇𝑢𝑏𝑒 𝑐𝑟𝑜𝑠𝑠 𝑠𝑒𝑐𝑡𝑖𝑜𝑛𝑎𝑙 𝑎𝑟𝑒𝑎 =
=𝜋×
= 1.5198 × 10−3 𝑚2
4
4
𝑚𝑒𝑎𝑛 𝑤𝑎𝑙𝑙 𝑡𝑒𝑚𝑝 =
𝑁𝑡
𝑛𝑢𝑚𝑏𝑒𝑟 𝑜𝑓 𝑝𝑎𝑠𝑠𝑒𝑠
86
=
= 43
2
𝑁𝑢𝑚𝑏𝑒𝑟 𝑜𝑓 𝑇𝑢𝑏𝑒𝑠 𝑝𝑒𝑟 𝑝𝑎𝑠𝑠 (𝑁𝑡𝑝𝑝 ) =
𝑚̇𝑡
𝑇𝑢𝑏𝑒 𝑠𝑖𝑑𝑒 𝑚𝑎𝑠𝑠 𝑣𝑒𝑙𝑜𝑐𝑖𝑡𝑦 (𝐺) =
𝐴
16.69
𝑘𝑔
=
= 10 982
∙ 𝑚2
0.0015198
𝑠
Density = 984.25 kg/ m3, k = 0.6515 W/mK and 𝜇 = 0.0004855 and Pr = 3.12
𝐺
∴ 𝑣 = = 11.16 𝑚/𝑠
𝑝
𝑅𝑒 =
𝑝𝑣𝑑
984.25 × 11.16 × 0.04399
=
𝜇
0.0004855
= 995 255
ℎ𝑖 𝑑𝑜
𝜇 0.14
= 𝑗ℎ 𝑅𝑒𝑃𝑟 0.33 ( )
𝑘𝑓
𝜇𝑤
𝜇
𝑁𝑒𝑔𝑙𝑒𝑐𝑡 ( )
𝜇𝑤
𝐿
3
=
= 68.19
𝑑𝑖 0.04399
∴ 𝑗ℎ 𝑖𝑠 𝑜𝑏𝑡𝑎𝑖𝑛𝑒𝑑 𝑓𝑟𝑜𝑚 𝑓𝑖𝑔𝑢𝑟𝑒 8 = 0.0018
ℎ𝑖 =
1
0.6515
× 0.0018 × 995 255 × 3.123
0.04399
= 38 769 𝑊/𝑚2 ∙ ℃
13
16. Overall coefficient


Assuming material is steel, therefore thermal conductivity = 45 𝑊/𝑚 ∙ ℃
obtained from table 4
Assuming cooling water is sea water.
Take the fouling coefficients from Table 5; steam condensate = 5000𝑊/𝑚2 ∙ ℃,
River water = 5 200 /𝑚2 ∙ ℃ .
𝑈𝑂 =
𝑈𝑂 =
1
𝑑𝑜
𝑑𝑜 𝑙𝑛 ( ⁄𝑑 )
1
1
𝑑
𝑑
𝑖
+
+
+ 𝑜 + 𝑜
ℎ𝑜 ℎ𝑑𝑜
2𝑘
𝑑𝑖 ℎ𝑖 𝑑𝑖 ℎ𝑑𝑖
1
0.0508
0.0508𝑙𝑛 (0.04399)
1
1
0.0508
0.0508
+
+
7269 + 5000 +
2(45)
0.04399 (38769) (0.04399)(5200)
= 1 499.96 𝑊/𝑚2 ∙ ℃
≈ 1 500 𝑊/𝑚2 ℃
This calculated value of the overall heat convection is equal to the estimated value in question
9. Therefore assumption is valid.
Due to the fact that the overall heat convection was equal to the assumed value, there is no
need to calculate pressure drop.
14
5. Conclusion
This paper demonstrates the application for the optimal design of a shell-and-tube heat
exchanger that will condense 3000 kg / h of steam. Approximate design methods for shell-andtube have been investigated and a generalized procedure has been developed to condense
3000 kg/h of steam and to find the maximum heat exchanger area and overall heat transfer
coefficient.
15
6. References
Dixit, S., Bhavsar, J.J. & Matawala, V.K., 2013. DESIGN AND EXPERIMENTAL ANALYSIS OF SPIRAL TUBE
HEAT. Mechanical and production engineering, 1(1), pp.37–42.
Holman, J. P. 2010. Heat Transfer, 10th edition.New York: McGraw Hill
Kuppan, T., 2013. Heat Exchanger Design Handbook 2nd ed., London: CRC Press.
Leong, K.C. et al., 1998. Shell and Tube Heat Exchanger Design Software for Educational Applications *. ,
14(3).
Ravagnani, M.A.S.S., Silva, A.P. & Caballero, J.A., 2009. Optimal Shell and Tube Heat Exchangers Design. ,
(1994).
Rodriguez, P., 1997. Selection of Materials for Heat Exchangers.
Selbas, R. & Reppich, M., 2006. A new design approach for shell-and-tube heat exchangers using genetic
algorithms from economic point of view. , 45, pp.268–275.
Shukla, A., Kumar, P. & Tiwari, D.R., 2015. Design Procedure of Shell and Tube Heat Exchanger. , 869(12),
pp.116–119.
Sinnott, R.K., 2005. Coulson & Richardsons Chemical Engineering Design,Oxford: Butterworth
Heneimann
Widiawati, M., 2015. Kolmetz Handbook Of Process Equipment Design HEAT EXCHANGER Selection of
Exchanger Components. , pp.1–31.
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7. Appendix
7.1.
Appendix A (Charts, (Sinnott, 2005))
Figure 5: Temperature correction factor: one shell pass; two or more even tube passes
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48
Figure 6: Shell-bundle clearance
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Figure 7: Shell-side heat-transfer factors, segmental baffles
Figure 8: Tube-side heat-transfer factor
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Appendix B (Tables of constants, (Sinnott, 2005))
Table 2: Approximate values of overall heat-transfer coefficients
Table 3: Constants for use in question 11
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Table 4: Conductivity of metals
Table 5: Fouling factors (coefficients), typical values
21