1. Shell and Tube Heat Exchangers

2. Goals: By the end of today’s lecture, you should be able to:
describe the common shell-and-tube HE designs
draw temperature profiles for parallel and counter-current flow in a
shell-and-tube HE
calculate the true mean temperature difference for a shell-and-tube
HE (use FG chart)
make heat transfer calculations for shell-and-tube HEs
describe how the inside and outside heat transfer coefficients are
determined for shell-and-tube HEs
use the Donohue equation to estimate ho in a multiple pass heat
exchanger
make heat transfer calculations for multiple pass shell-and-tube
heat exchangers

3. Outline:
I. Review
II. Shell-and-tube equipment
III. Rate equation and DTTM
IV. Ten Minute Problem - FG for multiple pass HE
V. Heat transfer coefficients
VI. Example Problem - Handout

4. I. Review Last time, we reviewed heat transfer in double pipe
(concentric pipe) heat exchangers.
We considered cases of parallel and countercurrent flow
of the hot and cold fluids in the concentric pipe design.
The basic equations required in the design of a heat exchanger
are the enthalpy balances on both fluid streams and a rate equation
that defines the heat transfer rate.

5. Enthalpy balances for fluids without phase change:
(hot stream) and (cold stream)
If a phase change occurs (the hot stream is condensed), then the heat of
condensation (vaporization) must be accounted for:
In most applications, the heat gained by the cold stream can be assumed to
equal the heat lost by the hot stream (i.e., qh = qc).

6. The rate of heat transfer for a concentric pipe heat exchanger with
parallel or countercurrent flow can be written as: or
where DTTM is the true mean temperature difference.
For concentric pipe heat exchangers, the true mean temperature
difference is equal to the log mean temperature difference (DTLM).

8. II. Shell-and-Tube Equipment
Concentric Pipe vs. Shell & Tube Heat Exchangers:
The simple double pipe heat exchanger is inadequate for flow rates that cannot
readily be handled in a few tubes. Double pipe heat exchangers are not used for
required heat exchange areas in excess of ft2. Several double pipe heat
exchangers can be used in parallel, but it proves more economical to have a single
shell serve for multiple tubes.

9. Typical Shell-and-Tube Heat Exchanger

10. Shell-and-tube heat exchangers are described based on the
number of passes the shell-side and tube-side fluids must undergo.
Exchangers are listed as 1-1, 1-2, 2-4, etc. in which the first number signifies
the number of passes for the shell-side fluid and the second number refers to the tube-side
fluid.

11. TEMA Designations

12. TEMA AES Exchanger

13. Baffles
How do baffles help? Where are they installed and which fluid is directly
affected?
Common practice is to cut away a segment having a height equal to one-
fourth the inside diameter of the shell. Such baffles are called 25 percent
baffles.

14. Baffle Arrangement

15. The RODbaffle heat exchanger design (Phillips Petroleum Co.)

16. Tube Bundles

17. Tube sizes Tubes Standard tube lengths are 8, 12, 16 and 20 ft.
Tubes are drawn to definite wall thickness in terms of BWG and true outside diameter (OD), and they are available in all common metals.

18. Tube Pitch The spacing between the tubes
(center to center) is referred to
as the tube pitch (PT). Triangular
or square pitch arrangements are
used. Unless the shell side tends
to foul badly, triangular pitch is
Used. Dimensions of standard
tubes are given in the Handout
and in MSH Appendix 6.

19. Tube Pitch

20. III. Rate equation and DTTM
The rate equation for a shell-and-tube heat exchanger is the same as
for a concentric pipe exchanger:
However, Ui and DTTM are evaluated somewhat differently for shell-and-tube
exchangers. We will first discuss how to evaluate DTTM and then a little later
in the notes we will discuss how to evaluate Ui for shell-and-tube exchangers.
In a shell-and-tube exchanger, the flow can be single or multipass. As a result,
the temperature profiles for the two fluids in a shell-and-tube heat exchanger
are more complex, as shown below.

21. DTlm Computation of DTTM:
For the concentric pipe heat exchanger, we showed the following (parallel and countercurrent flow):
DTTM =
When a fluid flows perpendicular to a heated or cooled tube bank, and if both of the fluid temperatures are varying, then the temperature conditions do not correspond to either parallel or countercurrent. Instead, this is called crossflow.
DTlm

22. FG * DTLM

23. The factor Z is the ratio of the fall in temperature of the shell side fluid to the rise
in temperature of the tube side fluid.
The factor hH is the heating effectiveness, or the ratio of the actual temperature
rise of the tube side fluid to the maximum possible temperature rise obtainable (if the
shell inlet end approach were zero, based on countercurrent flow).
From the given values of hH and Z, the factor FG can be read from the following figures:

24. Therefore, as with the concentric pipe heat exchanger, the true mean temperature
difference for the 1-1 exchanger is equal to the log mean temperature difference
(DTLM).
For multiple pass shell-and-tube designs, the flow is complex and the DTLM is less
than that for a pure countercurrent design.
We must account for the smaller temperature driving force using a correction factor,
FG, which is less than 1 and typically greater than 0.8.
The rate of heat transfer in multiple pass heat exchangers is written as:
where DTLM is the log mean temperature difference for pure countercurrent flow

25. 1-2 exchangers

26. 2-4 exchangers

27. IV. Ten Minute Problem -- FG for multiple pass HE
For a 2-4 heat exchanger with the cold fluid inside the tubes and the following
temperatures:
Tca = 85°F Tha = 200°F
Tcb = 125°F Thb = 100°F
(a) What is the true mean temperature difference?
(answer D TTM = 31.7°F)
(b) What exchanger area is required to cool 50,000 lbm/hr of product
(shell-side fluid) if the overall heat transfer coefficient is 100 Btu/hr-ft2-°F
and Cp for the product is 0.45 Btu/lbm-°F?
(answer A = 710 ft2)

28. V. Heat transfer coefficients
In a shell-and-tube exchanger, the shell-side and tube-side heat transfer
coefficients are of comparable importance and both must be large if a satisfactory
overall coefficient is to be attained.

31. Gb Gc Gb

32. Flow Area Through Baffle “Window” - SbDs
Baffle Cut
Tube Diameter Do
Baffle Window Area

33. Flow Area Across Tube Bundle - ScDo Ds p P

34. Exchanger Fouling
Electron microscope image showing fibers, dust, and other deposited material on a
residential air conditioner coil and a fouled water line in a water heater.

35. Exchanger Fouling

36. Example
A tubular exchanger with a 35 inch ID shell contains ¾ inch OD tubes 12 feet long on a 1 inch square pitch. Standard 25 percent cut baffles are spaced 12 inches apart. Liquid benzene at an average bulk temperature of 60 F is being heated in the shell side of the exchanger at a rate of 100,000 lb / hr. If the outside surfaces of the tubes are at 140 F, estimate the individual film coefficient of the benzene.