DME(10 TPD) Process Simulation Using Aspen Plus Release 12.1 Dr. Jungho Cho, Professor Department of Chemical Engineering Dong Yang University
Overall Flowsheet for DME Production Unit 18 TO FLARE 17 DA-103 DME ABSORBER EA-107 FA-107 21 EA-109 FA-109 EA-112 FA-110 31 26 DA-106 19 1 DA-104 CO2 STRIPPER DA-105 DME COLUMN MEOH RECOVERY COLUMN EA-103 EA-113 23 EA-110 33 28 Slide 2
DME Production Unit Simulation Using A+ 31 18 DA-106 DA-103 21 17 DA-104 DA-105 28 26 33 19 23 Slide 3
Flowsheet for Toluene Recovery Process Unit DA-103 DA-104 DA-105 DA-106 Stream 17 18 19 21 23 26 28 31 33 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
Slide 5 Vapor Vapor Mixed Phase 57.8774 20.040 52.0089 16.0500 2.37E-20 1.4602 7.0841 0.0148 0.0748 0.5795 20.2310 7.2161 63.3394 18 63.7119 48.336 59.3237 33.9587 3.009E-3 72.2858 17.0556 5.7143 9.63E-04 0.0185 4.1787 0.1919 0.5511 19 14.0000 3.192 3.3619 39.5540 3.084E-6 12.8111 3.236E-5 0.0170 0.3270 73.7331 3.3869 9.7249 21 110.2622 45.168 55.9618 33.6216 3.19E-03 76.6284 17.1306 6.0576 2.26E-15 4.34E-14 2.75E-04 8.19E-14 7.32E-14 23 46.0000 10.000 9.0580 46.0684 2.92E-06 99.9927 5.61E-03 1.40E-14 2.68E-13 1.70E-03 5.06E-13 4.52E-13 26 42.0432 33.480 43.7177 31.9039 2.64E-16 96.1336 1.4409 2.4255 7.27E-12 31 125.8043 35.136 46.9038 31.2179 3.81E-03 91.4268 1.3430 7.2264 6.77E-12 28 1.668 34.896 Flow rate (Ton/day) 21.8041 21.5106 MW (Kg/Kmol) 89.7695 3.1860 0.0560 26.8411 73.1028 33 45.0000 67.6140 2.64E-03 2.3854 19.4806 3.4594 0.0584 0.4620 19.2281 5.7191 49.2044 17 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
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-106 16 19 FL-102 Slide 6
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
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: 67.614 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
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
Material Balance Around DA-103 17 31 18 19 Phase Mixed Vapor Molar Percent H2 49.2044 63.3394 0.5511 CO 5.7191 7.2161 0.1919 CO2 19.2281 7.27E-12 20.2310 4.1787 CH4 0.4620 0.5795 0.0185 N2 0.0584 0.0748 9.63E-04 H2O 3.4594 2.4255 0.0148 5.7143 DME 19.4806 1.4409 7.0841 17.0556 MEA 2.3854 96.1336 1.4602 72.2858 MEOH 2.64E-03 2.64E-16 2.37E-20 3.009E-3 MW (Kg/Kmole) 21.5106 31.9039 16.0500 33.9587 Flow rate (K-mole/hr) 67.6140 43.7177 52.0089 59.3237 Flow rate (Ton/day) 34.896 33.480 20.040 48.336 Temperature ( o C) 45.0000 42.0432 57.8774 63.7119 Pressure (Kg/cm 2 ) 52.0330 1.333 48.0330 48.0330 Slide 10
2 nd Column: DA-104 (CO2 Stripper) EA-107 21 96.6x10 3 Kca/hr FA-107 61.6 o C 22.33Kg/cm 2 14.0 o C 23.03Kg/cm 2 19 DA-104 CO2 STRIPPER 98.5.6 o C 22.63Kg/cm 2 EA-108 165x10 3 Kca/hr 23 Slide 11
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
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
Material Balance Around CO2 Stripper 19 21 23 Phase Vapor Molar Percent H2 0.5511 9.7249 7.32E-14 CO 0.1919 3.3869 8.19E-14 CO2 4.1787 73.7331 2.75E-04 CH4 0.0185 0.3270 4.34E-14 N2 9.63E-04 0.0170 2.26E-15 H2O 5.7143 3.236E-5 6.0576 DME 17.0556 12.8111 17.1306 MEA 72.2858 3.084E-6 76.6284 MEOH 3.009E-3 3.19E-03 MW (Kg/Kmole) 33.9587 39.5540 33.6216 Flow rate (K-mole/hr) 59.3237 3.3619 55.9618 Flow rate (Ton/day) 48.336 3.192 45.168 Temperature ( o C) 63.7119 14.0000 110.2622 Pressure (Kg/cm 2 ) 48.0330 22.0330 22.6330 Slide 14
3 rd Column: DA-105 (DME Column) EA-109 129.4x10 3 Kca/hr FA-109 46.0 o C 10.83Kg/cm 2 48.2 o C 11.03Kg/cm 2 26 23 DA-105 DME COLUMN 87.0 o C 11.33Kg/cm 2 EA-110 127x10 3 Kca/hr 28 Slide 15
DME Column Simulation Primary objective of the DME column is to recovery DME as a top product. Slide 16
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
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
Material Balance Around DA-105 23 26 28 Phase Molar Percent H2 7.32E-14 4.52E-13 CO 8.19E-14 5.06E-13 CO2 2.75E-04 1.70E-03 6.77E-12 CH4 4.34E-14 2.68E-13 N2 2.26E-15 1.40E-14 H2O 6.0576 5.61E-03 7.2264 DME 17.1306 99.9927 1.3430 MEA 76.6284 2.92E-06 91.4268 MEOH 3.19E-03 3.81E-03 MW (Kg/Kmole) 33.6216 46.0684 31.2179 Flow rate (K-mole/hr) 55.9618 9.0580 46.9038 Flow rate (Ton/day) 45.168 10.000 35.136 Temperature ( o C) 110.2622 46.0000 125.8043 Pressure (Kg/cm 2 ) 22.6330 10.8330 11.0330 Slide 19
4 th Column: DA-106 (MEOH Recovery Column) EA-112 75.4 o C 1.53Kg/cm 2 469.4x10 3 Kcal/hr FA-110 42 o C 1.33Kg/cm 2 31 28 DA-106 MEOH Recovery COLUMN 81.3 o C 1.83Kg/cm 2 EA-113 382.4x10 3 Kcal/hr 33 Slide 20
MEOH Recovery Column Simulation Primary objective of the MEOH Recovery Column is to recovery MEOH as a top product. Slide 21
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
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
Material Balance Around DA-106 28 31 33 Phase Molar Percent H2 CO CO2 6.77E-12 7.27E-12 CH4 N2 H2O 7.2264 2.4255 73.1028 DME 1.3430 1.4409 MEA 91.4268 96.1336 26.8411 MEOH 3.81E-03 2.64E-16 0.0560 MW (Kg/Kmole) 31.2179 31.9039 21.8041 Flow rate (K-mole/hr) 46.9038 43.7177 3.1860 Flow rate (Ton/day) 35.136 33.480 1.668 Temperature ( o C) 125.8043 42.0432 89.7695 Pressure (Kg/cm 2 ) 11.0330 1.5330 Slide 24
The End. Slide 25