13-41
13-43
13-44
13-45
13.13
13.12
13-46
13.14
13-47
13.15
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. The UNIFAC model was
used for the phase equilibrium calculations, and the enthalpy calculations used the
ChemCAD Latent Heat method, which is equivalent to setting heats of mixing to zero.
The required minimum input information for this simulation is given below:
1. Flowsheet topology
13.19 Simulation of the Styrene process, Appendix B, Figure B.3.1 and Table B.3.1. The
simulation results are shown in the output following this page. The SRK model was used
for the phase equilibrium and the enthalpy calculations. The required minimum input
information for this simulation is given below:
1. Flowsheet topology
2. Specification of feed streams (Stream 1 and Stream 4)
13.20 Simulation of the Maleic Anhydride process, Appendix B, Figure B.5.1 and Table B.5.1.
The simulation results are shown in the output following this page. The ideal vapor
pressure model (Raoults Law) was used for the phase equilibrium and latent heat
model for enthalpies (zero heat of mixing). The required minimum input information for
this simulation is given below:
1. Flowsheet topology
13-51
Job Name: Ethylbenzene Date: 12/14/2008 Time: 13:38:22
FLOWSHEET SUMMARY
Equipment Label Stream Numbers
1 FIRE 127 -107
2 KREA 8 -9
3 KREA 11 -12
4 HTXR 118 -132
14 PUMP 123 -21
15 FIRE 134 -140
17 MIXE 12 13 –14
18 HTXR 111 -11
19 CSEP 145 -137 -15
20 HTXR 14 -118
Stream Connections
Stream Equipment Stream Equipment Stream Equipment
From To From To From To
1 24 15 19 29 117 22 24
2 10 16 28 118 20 4
3 22 23 17 29 27 119 13 8
13-52
CHEMCAD 5.6.0 Page 2
Job Name: Ethylbenzene Date: 12/14/2008 Time: 13:38:22
Calculation mode : Sequential
Flash algorithm : Normal
Equipment Calculation Sequence
Recycle Cut Streams
127 13
Recycle Convergence Method: Wegstein
13-53
CHEMCAD 5.6.0 Page 3
Job Name: Ethylbenzene Date: 12/14/2008 Time: 13:38:22
Overall Mass Balance kmol/h kg/h
Input Output Input Output
Benzene 97.169 8.683 7590.270 678.268
COMPONENTS
ID # Name Formula
1 40 Benzene C6H6
8 62 Water H2O
THERMODYNAMICS
K-value model : UNIFAC
No correction for vapor fugacity
13-54
CHEMCAD 5.6.0 Page 4
Job Name: Ethylbenzene Date: 12/14/2008 Time: 13:38:22
EQUIPMENT SUMMARIES
Fired Heater Summary
Equip. No. 1 15
Name
Pressure Drop kPa 15.0000 10.0000
Kinetic Reactor Summary
Equip. No. 2 3 7 25
Name
Reactor type 2 2 2 2
Reaction phase 1 1 1 1
Reaction Stoichiometrics and Parameters for unit no. 2
Reaction 1
RateConst = 1.6700e+006 Act.E = 2.2500e+004 Hrxn = 0.0000e+000
Comp Stoich. Exp.factor AdsorbFac. AdsorbE AdsorbExp.
1 -1.00e+000 0.0000e+000 0.0000e+000 0.0000e+000 0.0000e+000
Reaction 3
13-55
RateConst = 3.0000e+008 Act.E = 2.0000e+004 Hrxn = 0.0000e+000
Comp Stoich. Exp.factor AdsorbFac. AdsorbE AdsorbExp.
6 -1.00e+000 1.0000e+000 0.0000e+000 0.0000e+000 0.0000e+000
3 -2.00e+000 2.0000e+000 0.0000e+000 0.0000e+000 0.0000e+000
CHEMCAD 5.6.0 Page 5
Job Name: Ethylbenzene Date: 12/14/2008 Time: 13:38:22
EQUIPMENT SUMMARIES
Reaction 1
RateConst = 1.6700e+006 Act.E = 2.2500e+004 Hrxn = 0.0000e+000
Comp Stoich. Exp.factor AdsorbFac. AdsorbE AdsorbExp.
1 -1.00e+000 0.0000e+000 0.0000e+000 0.0000e+000 0.0000e+000
Reaction 2
RateConst = 1.0000e+006 Act.E = 2.2500e+004 Hrxn = 0.0000e+000
Comp Stoich. Exp.factor AdsorbFac. AdsorbE AdsorbExp.
2 -1.00e+000 1.0000e+000 0.0000e+000 0.0000e+000 0.0000e+000
Reaction Stoichiometrics and Parameters for unit no. 7
Reaction 1
RateConst = 1.3000e+007 Act.E = 2.5000e+004 Hrxn = 0.0000e+000
Comp Stoich. Exp.factor AdsorbFac. AdsorbE AdsorbExp.
Reaction Stoichiometrics and Parameters for unit no. 25
Reaction 1
RateConst = 1.6700e+006 Act.E = 2.2500e+004 Hrxn = 0.0000e+000
Comp Stoich. Exp.factor AdsorbFac. AdsorbE AdsorbExp.
1 -1.00e+000 0.0000e+000 0.0000e+000 0.0000e+000 0.0000e+000
13-56
Comp Stoich. Exp.factor AdsorbFac. AdsorbE AdsorbExp.
2 -1.00e+000 1.0000e+000 0.0000e+000 0.0000e+000 0.0000e+000
13-57
CHEMCAD 5.6.0 Page 6
Job Name: Ethylbenzene Date: 12/14/2008 Time: 13:38:22
EQUIPMENT SUMMARIES
6 -1.00e+000 1.0000e+000 0.0000e+000 0.0000e+000 0.0000e+000
Heat Exchanger Summary
Equip. No. 4 18 20 21
Name
1st Stream dp kPa 20.0000
1st Stream T Out C 170.0000 380.0000 280.0000 80.0000
Mixer Summary
Equip. No. 5 6 12 17
Name
13-58
CHEMCAD 5.6.0 Page 7
Job Name: Ethylbenzene Date: 12/14/2008 Time: 13:38:22
EQUIPMENT SUMMARIES
Flash Summary
Equip. No. 8
Name
Shortcut Distillaton Summary
Equip. No. 9
Name
Mode 2
Light key component 2.0000
Light key split 0.9900
Divider Summary
Equip. No. 10 11 22
Name
Split based on 0 0 1
13-59
CHEMCAD 5.6.0 Page 1
Job Name: Maleic Anhydride_JAS_2008 Date: 12/14/2008 Time: 15:53:41
FLOWSHEET SUMMARY
Equipment Label Stream Numbers
1 TOWR 9 8 –103 –102
2 KREA 6 15 -7 -16
3 HTXR 1 -110
Stream Connections
Stream Equipment Stream Equipment Stream Equipment
From To From To From To
1 3 10 12 93 13 14
2 15 11 11 9 100 4 5
Calculation mode : Sequential
Flash algorithm : Normal
Equipment Calculation Sequence
3 7 15 4 5 13 14 2 6 1 8 11 9 12 10
13-60
CHEMCAD 5.6.0 Page 2
Job Name: Maleic Anhydride_JAS_2008 Date: 12/14/2008 Time: 15:53:41
Recycle Convergence Tolerance
Flow rate 1.000E-003
Recycle calculation has converged.
Overall Mass Balance kmol/h kg/h
Input Output Input Output
Maleic Anhydride 0.000 47.447 0.000 4652.532
DibutylPhthalate 0.110 0.096 30.618 26.633
Nitrogen 4410.000 4410.000 123541.739 123541.727
COMPONENTS
ID # Name Formula
1 272 Maleic Anhydride C4H2O3
2 910 DibutylPhthalate C16H22O4
3 46 Nitrogen N2
THERMODYNAMICS
K-value model : Ideal Vapor Pressure
Enthalpy model : Latent Heat