DME(10 TPD) Process Simulation Using Aspen Plus Release Dr. Jungho Cho, Professor Department of Chemical Engineering Dong Yang University
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1 DME(10 TPD) Process Simulation Using Aspen Plus Release 12.1 Dr. Jungho Cho, Professor Department of Chemical Engineering Dong Yang University
2 Overall Flowsheet for DME Production Unit 18 TO FLARE 17 DA-103 DME ABSORBER EA-107 FA EA-109 FA-109 EA-112 FA DA DA-104 CO2 STRIPPER DA-105 DME COLUMN MEOH RECOVERY COLUMN EA-103 EA EA Slide 2
3 DME Production Unit Simulation Using A DA-106 DA DA-104 DA Slide 3
4 Flowsheet for Toluene Recovery Process Unit DA-103 DA-104 DA-105 DA-106 Stream Description DME Absorber CO2 Stripper DME Column MEOH Recovery Column Description DME Synthesis Reactor Outlet to DME Absorber Feed Stream DME Absorber OVHD Gas Stream to Flare DME Absorber BTMS Stream CO2 Stripper OVHD Gas Stream CO2 Stripper BTMS Stream DME Column OVHD Stream DME Column BTMS Stream MEOH Recovery Column OVHD Stream Recycled to DME Absorber MEOH Recovery Column BTMS Stream Slide 4
5 Slide 5 Vapor Vapor Mixed Phase E E E E E E E E E E E E E E E E E E E E E E Flow rate (Ton/day) MW (Kg/Kmol) E MEA MEOH CH4 N2 H2O Molar Percent H2 CO CO2 DME Flow rate (K-mole/hr) Temperature ( o C) Overall Material Balance Overall Material Balance
6 1 st Column: DA-103 (DME Absorber) 18 TO FLARE 31 MEOH T=57.9 o C P=48.03Kg/cm 2 DA-103 DME ABSORBER 17 T=63.5 o C P=48.03Kg/cm 2 EA FL-102 Slide 6
7 DME Absorber Simulation (DA-103) Primary objective of the absorber is to recovery DME as an absorber bottom product by using methanol as a solvent. Slide 7
8 DME Absorber Simulation Continued Consider the following absorber distillation to produce a purified toluene using sulfolane as a solvent. Feed1: Crude Feed (Refer to feedstock characterization) Feed2: Methanol Solvent 1) Solvent Feed Temperature: 45 o C 2) Flowrate: K-mole/hr DME Absorber Column 1) Number of Theoretical Stages: 7 3) Overall Tray Efficiencies: 4) Feed Tray Location: 7 6) Solvent Feed Tray Location: 1 Slide 8
9 DME Absorber Simulation Continued Selection of appropriate thermodynamic model for the simulation of DME absorber using methanol as a solvent is very important. NRTL (Non Random Two ) activity coefficient model was chosen to explain non-ideal phase behavior of liquid mixture between H2O, DME, methanol and MEA. Henry s law option was also selected for the calculation of non-condensible supercritical gases like H2, CO, CO2, CH4 and N2 in a liquid mixture. Slide 9
10 Material Balance Around DA Phase Mixed Vapor Molar Percent H CO CO E CH N E-04 H2O DME MEA MEOH 2.64E E E E-3 MW (Kg/Kmole) Flow rate (K-mole/hr) Flow rate (Ton/day) Temperature ( o C) Pressure (Kg/cm 2 ) Slide 10
11 2 nd Column: DA-104 (CO2 Stripper) EA x10 3 Kca/hr FA o C 22.33Kg/cm o C 23.03Kg/cm 2 19 DA-104 CO2 STRIPPER o C 22.63Kg/cm 2 EA x10 3 Kca/hr 23 Slide 11
12 CO2 Stripper Simulation Primary objective of the CO2 Stripper is to strip CO2 dissolved in the liquid feed stream at column top product. Slide 12
13 CO2 Stripper Simulation Continued Selection of appropriate thermodynamic model for the simulation of DME absorber using methanol as a solvent is very important. NRTL (Non Random Two ) activity coefficient model was chosen to explain non-ideal phase behavior of liquid mixture between H2O, DME, methanol and MEA. Henry s law option was also selected for the calculation of non-condensible supercritical gases like H2, CO, CO2, CH4 and N2 in a liquid mixture. Slide 13
14 Material Balance Around CO2 Stripper Phase Vapor Molar Percent H E-14 CO E-14 CO E-04 CH E-14 N2 9.63E E-15 H2O E DME MEA E MEOH 3.009E E-03 MW (Kg/Kmole) Flow rate (K-mole/hr) Flow rate (Ton/day) Temperature ( o C) Pressure (Kg/cm 2 ) Slide 14
15 3 rd Column: DA-105 (DME Column) EA x10 3 Kca/hr FA o C 10.83Kg/cm o C 11.03Kg/cm DA-105 DME COLUMN 87.0 o C 11.33Kg/cm 2 EA x10 3 Kca/hr 28 Slide 15
16 DME Column Simulation Primary objective of the DME column is to recovery DME as a top product. Slide 16
17 DME Column Simulation Continued Consider the following DME column to obtain a purified DME as a top product. Feed: CO2 Stripper Bottom Stream (Refer to feedstock characterization) 1) DME Product Purity = 99.9 by mole % DME Column 1) Number of Theoretical Stages: 20 3) Overall Tray Efficiencies: Can by estimated by correlation 4) Feed Tray Location: 11 Slide 17
18 DME Column Simulation Continued Selection of appropriate thermodynamic model for the simulation of DME Column is very important. NRTL (Non Random Two ) activity coefficient model was chosen to explain non-ideal phase behavior of liquid mixture between H2O, DME, methanol and MEA. Henry s law option was also selected for the calculation of non-condensible supercritical gases like H2, CO, CO2, CH4 and N2 in a liquid mixture. Slide 18
19 Material Balance Around DA Phase Molar Percent H2 7.32E E-13 CO 8.19E E-13 CO2 2.75E E E-12 CH4 4.34E E-13 N2 2.26E E-14 H2O E DME MEA E MEOH 3.19E E-03 MW (Kg/Kmole) Flow rate (K-mole/hr) Flow rate (Ton/day) Temperature ( o C) Pressure (Kg/cm 2 ) Slide 19
20 4 th Column: DA-106 (MEOH Recovery Column) EA o C 1.53Kg/cm x10 3 Kcal/hr FA o C 1.33Kg/cm DA-106 MEOH Recovery COLUMN 81.3 o C 1.83Kg/cm 2 EA x10 3 Kcal/hr 33 Slide 20
21 MEOH Recovery Column Simulation Primary objective of the MEOH Recovery Column is to recovery MEOH as a top product. Slide 21
22 MEOH Recovery Column Simulation Continued Consider the following MEOH Recovery Column to recover methanol stream as a top product. Feed: DME Column BTMS Stream (Refer to feedstock characterization) 1) Methanol Purity at Column Top: > 94 mole% MEOH Column 1) Number of Theoretical Stages: 20 3) Overall Tray Efficiencies: Can be Estimated by Correlation 4) Feed Tray Location: 11 Slide 22
23 MEOH Recovery Column Simulation Continued Selection of appropriate thermodynamic model for the simulation of MEOH Recovery Column is very important. NRTL (Non Random Two ) activity coefficient model was chosen to explain non-ideal phase behavior of liquid mixture between H2O, DME, methanol and MEA. Henry s law option was also used for the calculation of noncondensible supercritical gases in a mixed solvent. Slide 23
24 Material Balance Around DA Phase Molar Percent H2 CO CO2 6.77E E-12 CH4 N2 H2O DME MEA MEOH 3.81E E MW (Kg/Kmole) Flow rate (K-mole/hr) Flow rate (Ton/day) Temperature ( o C) Pressure (Kg/cm 2 ) Slide 24
25 The End. Slide 25
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