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Solutions Manual for Analysis, Synthesis,
and Design of Chemical Processes
Third Edition

Richard Turton
Richard C. Bailie
Wallace B. Whiting
Joseph A. Shaeiwitz

Prepared by Jessica W. Castillo

..
••
••
PRENTICE
HALL

Upper Saddle River, NJ • Boston' Indianapolis' San Francisco

New York· Toronto' Montreal· London· Munich· Paris· Madrid

Capetown· Sydney· Tokyo· Singapore. Mexico City
The author and publisher have taken care in the preparation of this book, but make no expressed
or implied warranty of any kind and assume no responsibility for errors or omissions. No liability
is assumed for incidental or consequential damages in connection with or arising out of the use
of the information or programs contained herein.
Visit us on the Web: www.informit.com/ph
Copyright © 2009, Pearson Education, Inc.
This work is protected by United States copyright laws and is provided solely for the use of
instructors in tcaching their courses and assessing student learning. Dissemination or sale of any
part of this work (including on the World Wide Web) will destroy the integrity of the work and is
not permitted. The work and materials from it should never be made available to students except
by instructors using the accompanying text in their classes. All recipients of this work are
expected to abide by these restrictions and to honor the intended pedagogical purposes and the
needs of other instructors who rely on these materials.

ISBN-13: 978-0-13-702385-1
ISBN-IO: 0-13-702385-5
Text printed in the United States at OPM in Laflin, Pennsylvania.
First printing, January 2009
 Chapter 1

1.1 Block Flow Diagram (BFD)

Process Flow Diagram (PFD)
Piping and Instrument Diagrams (P&ID)

(a) PFD
(b) BFD
(c) PFD or P&ID
(d) P&ID
(e) P&ID

1.2 P&ID

1.3 It is important for a process engineer to be able to review a 3-dimensional model prior to
the construction phase to check for clearance, accessibility, and layout of equipment,
piping, and instrumentation.

1.4 (1) Clearance for tube bundle removal on a heat exchanger.

(2) NPSH on a pump – affects the vertical separation of feed vessel and pump inlet.
(3) Accessibility of an instrument for an operator – must be able to read a PI or
change/move a valve.
(4) Separation between equipment for safety reasons – reactors and compressors.
(5) Crane access for removing equipment.
(6) Vertical positioning of equipment to allow for gravity flow of liquid.
(7) Hydrostatic head for thermosiphon reboiler – affects height of column skirt.

1.5 Plastic models are no longer made because they are too expensive and difficult to
change/revise. These models have been replaced with virtual/E-model using 3-D CAD.
Both types of model allow revision of critical equipment and instrument placement to
ensure access, operability, and safety.

1.6 Another reason to elevate the bottom of a tower is to provide enough hydrostatic head
driving force to operate a thermosiphon reboiler.

1-1
1.7 (a) PFD or P&ID
(b) PFD
(c) PFD
(d) P&ID
(e) BFD (or all PFDs)

1.8 A pipe rack provides a clear path for piping within and between processes. It keeps piping
off the ground to eliminate tripping hazards and elevates it above roads to allow vehicle
access.

1.9 A structure – mounted vertical plant layout is preferred when land is at a premium and the
process must have a small foot print. The disadvantage is that it is more costly because of
the additional structural steel.

1.10 (a) BFD – No change

PFD – Efficiency changed on fired heater, resize any heat exchanger used to extract
heat from the flue gas (economizer)
P&ID – Resize fuel and combustion air lines and instrumentation for utilities to fired
heater. Changes for design changed of economizer (if present)
(b) BFD – Change flow of waste stream in overall material balance
PFD – Change stream table
P&ID – Change pipe size and any instrumentation for this process line
(c) BFD – No change
PFD – Add a spare drive, e.g. D-301 → D-301 A/B
P&ID – Add parallel drive
(d) BFD – No change
PFD – No change
P&ID – Note changes of valves on diagram

1.11 (a) A new vessel number need not be used, but it would be good practice to add a letter to
donate a new vessel, e.g. V-203 → V-203N. This will enable an engineer to locate the
new process vessel sheet and vendor information.
(b) P&ID definitely
PFD change/add the identifying letter.

1-2
1.12

1-3
1.13 (a) (i) Open globe valve D
(ii) Shut off gate valves A and C
(iii)Open gate valve E and drain contents of isolated line to sewer
(iv) Perform necessary maintenance on control valve B
(v) Reconnect control valve B and close gate valve E
(vi) Open gate valves A and C
(vii) Close globe valve D
(b) Drain from valve E can go to regular or oily water sewer.
(c) Replacing valve D with a gate valve would not be a good idea because we loose
the ability to control the flow of process fluid during the maintenance operation.
(d) If valve D is eliminated then the process must be shut down every time
maintenance is required on the control valve.

1-4
1.14

1.15

1-5
1.16 (a) For a pump with a large NPSH – the vertical distance between the feed vessel and the
pump inlet must be large in order to provide the static head required to avoid cavitating the
pump.
b) Place the overhead condenser vertically above the reflux drum – the bottom shell
outlet on the condenser should feed directly into the vertical drum.

c) Pumps and control valves should always be placed either at ground level (always for
pumps) or near a platform (sometimes control valves) to allow access for maintenance.
d) Arrange shell and tube exchangers so that no other equipment or structural steel
impedes the removal of the bundle.

e) This is why we have pipe racks – never have pipe runs on the ground. Always elevate
pipes and place on rack.
f) Locate plant to the east of major communities.

1.17
1-6
 ⎛1⎞
1.17 HT area of 1 tube = πDL = π ⎜ ⎟(12 ft ) = 3.142 ft2
⎝12 ⎠
⎛ 3.2808 ft ⎞ 2 ⎛ 1 ⎞
Number of tubes = (145 m2 ) ⋅ ⎜ ⎟⎜ 2⎟
= 497 tubes
⎝ m ⎠ ⎝ 3.142 ft ⎠
Use a 1 1/4 inch square pitch ⇒

π⎛ 1m ⎞ ⎛ m ⎞2
2

Fractional area of the tubes = ⎜ ⎟ = 0.5027⎜ ⎟

4 ⎝1.25 in ⎠ ⎝ in ⎠

AVAP = 3 ALIQ ∴CSASHELL = 4 ALIQ

⎛ 497 ⎞⎛ in ⎞ 2 ⎛ π ⎞
ALIQ = ⎜ ⎟⎜ ⎟ ⎜ ⎟(1 m) = 777 in
2 2
⎝ 0.5027 ⎠⎝ m ⎠ ⎝ 4 ⎠

π
CSASHELL = (4 )(777) = 3108 in 2 ⇒ D2SHELL = 3108 in 2
4
(4 )(3108 in 2
) = 62.9 in = 1.598 m
DSHELL =
π

Length of Heat Exchanger = (2 + 12 + 2) ft = 16 ft = 4.877 m

Foot Print = 1.598 × 4.877 m

1-7
1.18 From Table 1.11 towers and reactors should have a minimum separation of 15 feet or 4.6
meters. No other restrictions apply. See sketch for details.

1-8
1.19

1-9
1.20

1-10
1.21 (a) A temperature (sensing) element (TE) in the plant is connected via a capillary line to
a temperature transmitter (TT) also located in the plant. The TT sends an electrical
signal to a temperature indicator controller (TIC) located on the front of a panel in the
control room.
(b) A pressure switch (PS) located in the plant sends an electrical signal to …
(c) A pressure control valve (PCV) located in the plant is connected by a pneumatic (air)
line to the valve stem.
(d) A low pressure alarm (PAL) located on the front of a panel in the control room
receives an electrical signal from …
(e) A high level alarm (LAH) located on the front of a panel in the control room receives
a signal via a capillary line.

1-11
1.22
2” sch 40 CS

V-302 LE LT LIC LY

PAL LAH

2” sch 40 CS
4” sch 40 CS

3
1 To wastewater treatment
2 To chemical sewer
P-402 3 Vent to flare
P-401
2 2

List of Errors
1. Pipe inlet always larger than pipe outlet due to NPSH
issues
= Error 2. Drains to chemical sewer and vent to flare
3. Double-block and bleed needed on control valve
4. Arrows must be consistent with flow of liquid through
2” sch 40 CS pumps
5. Pumps in parallel have A and B designation
3 6. Pneumatic actuation of valve stem on cv is usual
7. Level alarm low not pressure alarm low

V-302 LE LT LIC LY

LAL LAH Corrected

P&ID
4” sch 40 CS
2” sch 40 CS

1 To wastewater treatment
2 To chemical sewer
2
P-401B 3 Vent to flare
P-401A
2 2

1-12
 Chapter 2

2.1 The five elements of the Hierarchy of Process Design are:

a. Batch or continuous process
b. Input – output structure of process
c. Recycle structure of process
d. General separation structure of process
e. Heat-exchanger network/process energy recovery

2.2 a. Separate/purify unreacted feed and recycle – use when separation is feasible.
b. Recycle without separation but with purge – when separation of unused reactants is
infeasible/uneconomic. Purge is needed to stop build up of product or inerts.
c. Recycle without separation or purge – product/byproduct must react further through
equilibrium reaction.

2.3 Batch preferred over continuous when: small quantities required, batch-to-batch
accountabilities required, seasonal demand for product or feed stock availability, need to
produce multiple products using the same equipment, very slow reactions, and high
equipment fouling.

2.4 One example is the addition of steam to a catalytic reaction using hydrocarbon feeds.
Examples are given in Appendix B (styrene, acrylic acid.) In the styrene process,
superheated steam is added to provide energy for the desired endothermic reaction and to
force the equilibrium towards styrene product. In the acrylic acid example, steam is added
to the feed of propylene and air to act as thermal ballast (absorb the heat of reaction and
regulate the temperature), and it also serves as an anti-coking agent – preventing coking
reactions that deactivate the catalyst.

2-1
2.5 Reasons for purifying a feed material prior to feeding it to a process include:
a. If impurity foul or poison a catalyst used in the process.
e.g. Remove trace sulfur compounds in natural gas prior to sending to the steam
reforming reactor to produce hydrogen.

CH 4 + H 2 0 → CO + 3H 2
Remove trace sulfur
Platinum catalyst v. susceptible to
sulfur poisoning

b. If impurities react to form difficult-to-separate or hazardous products/byproducts.

e.g. Production of isocyanates using phosgene. Production of phosgene is
CO + Cl2 → COCl2
The carbon monoxide is formed via steam reforming of CH4 to give CO + H2. H2 must
be removed from CO prior to reaction with Cl2 to form HCl, which is highly corrosive
and causes many problems in the downstream processes.

c. If the impurity is present in large quantities then it may be better to remove the impurity
rather than having to size all the down stream equipment to handle the large flow of
inert material.
e.g. One example is suing oxygen rather than air to fire a combustion or gasification
processes. Removing nitrogen reduces equipment size and makes the removal of CO2
and H2S much easier because these species are more concentrated.

2.6 IGCC H 2O + Ca H b Sc Od N e + O2 → pCO2 + qH 2 + rH 2O + sCO + tNH 3 + uH 2 S

Coal

In modern IGCC plants, coal is partially oxidized (gasified) to produce synthesis gas CO
+ H2 and other compounds. Prior to combusting the synthesis gas in a turbine, it must be
“cleaned” or H2S and CO2 (if carbon capture is to be employed.) Both H2S and CO2 are
acid gases that are removed by one of a variety of physical or chemical absorption
schemes. By removing nitrogen from the air, the raw synthesis gas stream is much smaller
making the acid gas removal much easier. In fact, when CO2 removal is required IGCC is
the preferred technology, i.e. the cheapest.

2-2
2.7 Ethylebenzene Process

a. Single pass conversion of benzene

kmol
Benzene in reactor feed (stream 3) = 226.51
h
kmol
Benzene in reactor effluent (stream 14) = 177.85
h
kmol
177.85
X sp = 1− h = 21.5%
kmol
226.51
h

b. Single pass conversion of ethylene

kmol
Ethylene in reactor feed (stream 2) = 93.0
h
kmol
Ethylene in reactor effluent (stream 14) = 0.54
h
kmol
0.54
X sp = 1− h = 99.4%
kmol
93.0
h
c. Overall conversion of benzene
kmol
Benzene entering process (stream 1) = 97.0
h
kmol
Benzene leaving process (stream 15 and 19) = 8.38 + 0.17
h
kmol
8.55
X ov = 1− h = 91.2%
kmol
97.0
h
d. Overall conversion of ethylene
kmol
Ethylene entering process (stream 2) = 93.0
h
kmol
Ethylene leaving process (stream 15 and 19) = 0.54 + 0
h
kmol
0.54
X ov = 1− h = 99.4%
kmol
93.0
h

2-3
2.8 Separation of G from reactor effluent may or may not be difficult. (a) If G reacts to form a
heavier (higher molecular weight) compound then separation may be relatively easy using
a flash absorber or distillation and recycle can be achieved easily. (b) If process is to be
viable then G must be separable from the product. If inerts enter with G or gaseous by-
products are formed then separation of G may not be possible but recycling with a purge
should be tried. In either case the statement is not true.

2.9 Pharmaceutical products are manufactured using batch process because:

a. they are usually required in small quantities
b. batch-to-batch accountability and tracking are required by the Food & Drug
Administration (FDA)
c. usually standardized equipment is used for many pharmaceutical products and
campaigns are run to produce each product – this lends itself to batch operation.

2-4
2.10 a. Single pass conversion of ethylbenzene
kmol
Ethylbenzene in reactor feed (stream 9) = 512.7
h
kmol
Ethylbenzene in reactor effluent (stream 12) = 336.36
h
kmol
336.36
Single pass conversion = 1− h = 34.4%
kmol
512.7
h
b. Overall conversion of ethylbenzene
kmol
Ethylbenzene entering process (stream 1) = 180
h
kmol
Ethylbenzene leaving process (stream 19, 26, 27 & 28) = 3.36 + 0.34 = 3.70
h
kmol
3.70
Overall conversion = 1− h = 97.9%
kmol
180
h
c. Yield of styrene
kmol
Moles of ethylbenzene required to produce styrene = 119.3
h
kmol
Moles of ethylbenzene fed to process (stream 1) = 180
h
kmol
119.3
Yield = h = 66.3%
kmol
180
h

Possible strategies to increase the yield of styrene are

(i) Increase steam content of reactor feed – this pushes the desired equilibrium
reaction to the right.

(ii) Increasing the temperature also pushes the equilibrium to right but increases
benzene and toluene production.

(iii) Remove hydrogen in effluent from each reactor – this will push the
equilibrium of the desired reaction to the right and reduce the production of
toluene from the third reaction – use a membrane separator, shown on
following page.

2-5
2-6
2.11 Route 1: 2A → S + R

Key features are that no light components (non-condensables) are formed and only one
reactant is used. Therefore, separation of A, R, and S can take place using distillation
columns.

Route 2: A + H2 → S + CH4

Unlike Route 1, this process route requires separation of the non-condensables from A and
S. If hydrogen is used in great excess (as with the toluene HDA process), then a recycle
and purge of the light gas stream will be required. Otherwise, if hydrogen conversion is
high, the unreacted hydrogen along with the methane may be vented directly to fuel gas.

Route 1 – PFD sketch

A S
Tower 1
Tower 2
Reactor

Recycled A

Route 2 – PFD sketch – gas recycle shown dotted since it is only needed if H2 is used in
(considerable) excess and must be recycled.
H2 + CH4
Compressor
A S

Reactor Tower

Gas Separator
Recycled A

2-7
Route 1 is better since:
• Simpler PFD
• No gas recycle (no recycle compressor)
• No build up of inerts (CH4) so recycle stream is not as large
• All products are valuable – fuel gas in Route 2 has a low value

2-8
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