Archives: Solution Manual

23-20 Background Information on Problems 23.17 – 23.20 23-21 23.17 23-22 23.17 (contd) 23-23 23.18 23-24 23.18 (contd) 23.19 See Problem 23.18 for: a) Flowsheet of fluid bed reactor b) Calculation strategy c) Calculation for V = 7.49 m3 23-25 […]

Chapter 23 23.1 The main reason is the requirement for large reactors in order to obtain very high conversions. If the reaction rates are very high for the conditions used (for example the combustion of a fuel in air or […]

22-18 22.16 22-19 22.16 (cont’d) Solution to Problem 22.16 22-20 22.17 22-21 22.17 (cont’d) Solution to Problem 22.17 22.17 (cont’d) 22-22 22-23 19.18 (a) Acrylic Acid reboiled at 89°C = 362 K (b) Ptop Pbottom P Ptop 15.92 kPa 9.5 […]

22-1 Chapter 22 22.1 From Figure B.10.1, it can be seen that the molten salt is heated by a fired heater in the circulating loop. This implies that heat is added to the reactor, i.e., the reaction is 22.2 Pressure […]

21-32 21.34 (contd) 21-33 21.34 (contd) 21-34 21.35 (see supplemental information on page 21-30) 21-35 21.35 (contd) 21-36 21.35 (contd) 21-37 18.36 Cooling Water Energy Balance MCW1CP140 C 30 C MCW 2CP2T30 C T30 C MCW1 MCW 2 40 C […]

21-21 21.29 21-22 21.29 (contd) 21-23 21.30 21-24 21.30 (contd) 21.30 21-25 21.31 21-26 21.31 (contd) 21.31 21-27 21.32 21-28 21.33 21-29 21.33 (contd) 21-30 Supplementary Information for Problems 21.34 and 21.35 21-31 21.34 (see supplemental information on page 21-30)

21-1 Chapter 21 21.1 A pump curve shows the relationship between pressure head and volumetric flowrate through a pump 21.2 All depends on the system curve, so the statement is false since parallel or series arrangements could give higher scale […]

Chapter 20 20.1 Second order reaction: r kCA 2; k Ae E RT If ideal Ci PiRT if ideal 220ºC = 493K 250ºC = 523K r2 r 1 A2 A1 e E R 1 T2 1 T1CA2 2 CA1 2 […]

19-1 Chapter 19 19.1 (a) Fluidized Bed (b) Turbine (d) Stripper Input Output Frictional loss Liquid Input Vapor Out p ut Vapor Input Liquid Output Possibly heat added (c) Pump Input Output Work Input Output Work 19-2 (e) Adiabatic Batch […]

18-13 18.6 18-14 FIC FIC 18-15 19.7 18.7 18-16 TIC LIC 18.8 18-17 FIC set point 18-18 1 8.9 LIC LIC FIC TIC 18-19 FIC 1 8. 1 0 18-20 18-21 18.11 As per B.5, C-601 is an electrically driven […]

18-1 Chapter 18 18.1 a. 18-2 b. 18-3 18-4 18-5 18.2 18-6 18.3 PIC LIC 18-7 18-8 PIC FIC LIC 18-9 18.4 18-10 18-11 TIC 18-12 18.5 FIC LIC YIC

17-1 Chapter 17 17.1 Transient response of a variable can be obtained from a dynamic simulation, not from a steady state simulation. 17.2 The flow through a flow device can be related through the pressure drop across it. This creates […]

16-12 It can be seen in the UAM shown below that the upper two designs exceed the high temperature limit when the flowrate is decreased by 30%. Both the lower designs satisfy the design requirement of 40% conversion under base […]

16-1 Chapter 16 16.1 Process simulators generate an incidence matrix based on the process flowsheet and then perform row operations to determine partitioning and precedence ordering. 16.2 In Stream 1, the number of variables for which a good guess is […]

15-39 (c) Above pinch theory says 4 exchangers but can try “direct match” HU 40 1 100 2 120 3 160 4 100 40 120 100 Below pinch 3 exchangers 2 180 CU 240 3 100 160 100 1 160 […]

15-21 15.16 (a) QB = (4 + 3 – 3)(20) = 80 kW QC = (4 + 3 – 3 – 5)(50) = – 50 kW From interval A ( 4 )( 50 ) – ( mc p ) 3 […]

15-1 Chapter 15 15.1 Costs affected by changing the min temp approach for a HEN are 15.2 By decreasing the Tmin in a HEN, the process-process heat exchangers at the pinch will require larger areas and will therefore be more […]

14-13 14.13 – Two product batch sequencing Optimum Solution is to just make Product B 14-14 14.14 –Three product batch sequencing 14-15 14-16 14-17 14-18 14-19 14-20 14-21 14.6 8.3 14-22 14-23

14-1 Chapter 14 14.1 Describe a Pareto analysis. When is it used? Strictly speaking, a Pareto analysis is statistical technique but we use it here in the more 14.2 What is the difference between parametric optimization and topological optimization? List […]

13-97 CHEMCAD 5.6.0 Page 10 Job Name: formalin_JAS_2008 Date: 12/14/2008 Time: 14:45:38 FLOW SUMMARIES Stream No. 1 2 3 4 Stream Name Temp C 25.0000 30.0000 40.6637 40.7822 Pres kPa 101.3250 120.0000 101.3250 300.0000 Stream No. 5 6 7 8 […]

13-81 CHEMCAD 5.6.0 Page 5 Job Name: ethylene oxide with recycle Date: 12/14/2008 Time: 14:37:10 EQUIPMENT SUMMARIES Mixer Summary Equip. No. 6 21 22 Name Output Pressure bar 26.8000 90.0000 Valve Summary Kinetic Reactor Summary Equip. No. 9 15 Name […]

13-61 CHEMCAD 5.6.0 Page 3 Job Name: Maleic Anhydride_JAS_2008 Date: 12/14/2008 Time: 15:53:41 EQUIPMENT SUMMARIES Towr Rigorous Distillation Summary Equip. No. 1 Condenser mode 5 Condenser spec. 0.5000 Cond. comp i 1 Reboiler mode 5 Reboiler spec. 1.0000 Reboiler comp […]

13-41 13-42 13-43 13-44 13-45 13.13 13.12 13-46 13.14 13-47 13.15 13-48 13-49 13.16 13.17 13-50 13.18 Simulation of the Ethylbenzene process, Appendix B, Figure B.2.1 and Table B.2.1. The simulation results are shown in the output following this page. […]

13-21 13.9 Simulation of the IPA to acetone Process, Appendix B, Figure B.10.1 and Tables B . 1 0. 1 and B . 1 0. 2 13-22 13-23 13-24 13-25 13-26 13-27 13-28 13-29 13-30 13.10 13-31 13-32 13-33 13-34 […]

13-1 Chapter 13 13.1 Long-range forces are included in the expression for the excess Gibbs energy 13.2 The ionic interactions affect the excess Gibbs energy of an electrolyte system through short-range and long-range forces as shown in Eqn 13.34. This, […]

12-32 12-33 12-34 12-35 12-36 12-37 12-38 12-39 12-40 12.18 Equation 12.1 applies for any “theoretical simple sequence” separation, i.e., where each separation unit makes a perfect split between components. These sequences can be for 12.19 In the derivation of […]

12-21 12-22 12-23 12-24 12-25 12-26 12-27 12-28 12-29 12-30 12-31

12-1 Chapter 12 12-2 12-3 12-4 12-5 12-6 12-7 12-8 12-9 12.13 12-10 12-11 12-12 12-13 12-14 12-15 12-16 12-17 12-18 12-19 12-20