DME(10 TPD) Process DME(10 TPD) Process
Simulation Simulation
Using Using
Aspen Plus Release 12.1 Aspen Plus Release 12.1
Dr. Jungho Cho, Professor
Department of Chemical Engineering
Dong Yang University
Overall
Overall Flowsheet Flowsheet for DME Production Unit for DME Production Unit
DME
ABSORBER
TO FLARE
17
19 18
DA-103
1
21
CO2
STRIPPER DA-104
EA-103 EA-107
FA-107
23
26
DME COLUMN DA-105
EA-110 EA-109
FA-109
28
31
MEOH
RECOVERY COLUMN DA-106
EA-113 EA-112
FA-110
33
Slide 3
DA-103
DA-104
DA-105
DA-106
17
18
19
21
23
26 28
33 31
DME Production Unit Simulation Using A+
DME Production Unit Simulation Using A+
Flowsheet for Toluene Recovery Process Flowsheet for Toluene Recovery Process
DME Absorber OVHD Gas Stream to Flare 18
DME Absorber BTMS Stream 19
MEOH Recovery Column BTMS Stream 33
MEOH Recovery Column OVHD Stream Recycled to DME Absorber 31
DME Column BTMS Stream 28
DME Column OVHD Stream 26
CO2 Stripper BTMS Stream 23
CO2 Stripper OVHD Gas Stream 21
DME Synthesis Reactor Outlet to DME Absorber Feed Stream 17
Description Stream
MEOH Recovery Column DA-106
DME Column DA-105
CO2 Stripper DA-104
DME Absorber DA-103
Description
Unit
Slide 5
Liquid Liquid
Liquid Liquid
Liquid Vapor
Liquid 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 0.0000 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 0.0000 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 0.0000 0.0000 7.27E-12 0.0000 0.0000 31
125.8043 35.136 46.9038 31.2179 3.81E-03 91.4268 1.3430 7.2264 0.0000 0.0000 6.77E-12 0.0000 0.0000 28
1.668 34.896
Flow rate (Ton/day)
21.8041 21.5106
MW (Kg/Kmol)
89.7695 3.1860 0.0560 26.8411 0.0000 73.1028 0.0000 0.0000 0.0000 0.0000 0.0000 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 (oC)
Overall Material Balance
Overall Material Balance
1 1 st st Column: DA Column: DA - - 103 (DME Absorber) 103 (DME Absorber)
DME ABSORBER
TO FLARE
17
19 EA-106
18
FL-102 16
31 MEOH
DA-103
T=57.9
oC
P=48.03Kg/cm
2T=63.5
oC
P=48.03Kg/cm
2Slide 7
DME Absorber Simulation (DA
DME Absorber Simulation (DA - - 103) 103)
Primary objective of the absorber is to recovery DME as an absorber bottom product by using methanol as a
solvent.
Consider the following absorber distillation to produce a purified toluene using sulfolane as a solvent.
y Feed1: Crude Feed (Refer to feedstock characterization) y Feed2: Methanol Solvent
1) Solvent Feed Temperature: 45 o C 2) Flowrate: 67.614 K-mole/hr
y DME Absorber Column
1) Number of Theoretical Stages: 7 3) Overall Tray Efficiencies:
4) Feed Tray Location: 7
6) Solvent Feed Tray Location: 1
DME Absorber Simulation
DME Absorber Simulation Continued Continued
Slide 9
Selection of appropriate thermodynamic model for the
simulation of DME absorber using methanol as a solvent is very important.
y NRTL (Non Random Two Liquid) activity coefficient
model was chosen to explain non-ideal phase behavior of liquid mixture between H2O, DME, methanol and
MEA.
y 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.
DME Absorber Simulation
DME Absorber Simulation Continued Continued
Material Balance Around DA
Material Balance Around DA - - 103 103
48.0330 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 Vapor 18
48.0330 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 Liquid 19
1.333 42.0432 33.480 43.7177 31.9039 2.64E-16 96.1336 1.4409 2.4255 0.0000 0.0000 7.27E-12 0.0000 0.0000 Liquid 31
52.0330 45.0000 34.896 67.6140 21.5106 2.64E-03 2.3854 19.4806 3.4594 0.0584 0.4620 19.2281 5.7191 49.2044 Mixed 17
Flow rate (Ton/day) MW (Kg/Kmole) Phase
MEA MEOH CH4 N2 H2O
Molar Percent H2
CO CO2
DME
Flow rate (K-mole/hr)
Pressure (Kg/cm
2)
Temperature (
oC)
Slide 11
2 2 nd nd Column: DA Column: DA - - 104 (CO2 Stripper) 104 (CO2 Stripper)
19
21
CO2 STRIPPER DA-104
EA-108 EA-107
FA-107
23
61.6
oC
22.33Kg/cm
298.5.6
oC 22.63Kg/cm
214.0
oC
23.03Kg/cm
296.6x10
3Kca/hr
165x10
3Kca/hr
CO2 Stripper Simulation CO2 Stripper Simulation
Primary objective of the CO2 Stripper is to strip CO2
dissolved in the liquid feed stream at column top product.
Slide 13
Selection of appropriate thermodynamic model for the
simulation of DME absorber using methanol as a solvent is very important.
y NRTL (Non Random Two Liquid) activity coefficient
model was chosen to explain non-ideal phase behavior of liquid mixture between H2O, DME, methanol and
MEA.
y 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.
CO2 Stripper Simulation
CO2 Stripper Simulation Continued Continued
Material Balance Around CO2 Stripper Material Balance Around CO2 Stripper
48.0330 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 Liquid 19
22.0330 14.0000 3.192 3.3619 39.5540 0.0000 3.084E-6 12.8111 3.236E-5 0.0170 0.3270 73.7331 3.3869 9.7249 Vapor 21
22.6330 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 Liquid 23
Pressure (Kg/cm
2) Temperature (
oC) Flow rate (Ton/day) Flow rate (K-mole/hr) MW (Kg/Kmole)
MEOH MEA DME H2O N2 CH4 CO2 CO H2
Molar Percent
Phase
Slide 15
3 3 rd rd Column: DA Column: DA - - 105 (DME Column) 105 (DME Column)
23
26
DME COLUMN DA-105
EA-110 EA-109
FA-109
28
87.0
oC
11.33Kg/cm
248.2
oC
11.03Kg/cm
2127x10
3Kca/hr
46.0
oC
10.83Kg/cm
2129.4x10
3Kca/hr
DME Column Simulation DME Column Simulation
Primary objective of the DME column is to recovery DME
as a top product.
Slide 17
Consider the following DME column to obtain a purified DME as a top product.
y Feed: CO2 Stripper Bottom Stream (Refer to feedstock characterization)
1) DME Product Purity = 99.9 by mole % y DME Column
1) Number of Theoretical Stages: 20
3) Overall Tray Efficiencies: Can by estimated by correlation 4) Feed Tray Location: 11
DME Column Simulation
DME Column Simulation Continued Continued
Selection of appropriate thermodynamic model for the simulation of DME Column is very important.
y NRTL (Non Random Two Liquid) activity coefficient
model was chosen to explain non-ideal phase behavior of liquid mixture between H2O, DME, methanol and
MEA.
y 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.
DME Column Simulation
DME Column Simulation Continued Continued
Slide 19
Material Balance Around DA
Material Balance Around DA - - 105 105
22.6330 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 Liquid 23
10.8330 46.0000 10.000 9.0580 46.0684 0.0000 2.92E-06 99.9927 5.61E-03 1.40E-14 2.68E-13 1.70E-03 5.06E-13 4.52E-13 Liquid 26
11.0330 125.8043 35.136 46.9038 31.2179 3.81E-03 91.4268 1.3430 7.2264 0.0000 0.0000 6.77E-12 0.0000 0.0000 Liquid 28
Pressure (Kg/cm
2) Temperature (
oC) Flow rate (Ton/day) Flow rate (K-mole/hr) MW (Kg/Kmole)
MEOH MEA DME H2O N2 CH4 CO2 CO H2
Molar Percent
Phase
4 4 th th Column: DA Column: DA - - 106 (MEOH Recovery Column) 106 (MEOH Recovery Column)
28
31
MEOH Recovery COLUMN DA-106
EA-113 EA-112
FA-110
33
75.4
oC
1.53Kg/cm
281.3
oC
1.83Kg/cm
242
oC
1.33Kg/cm
2469.4x10
3Kcal/hr
382.4x10
3Kcal/hr
Slide 21
MEOH Recovery Column Simulation MEOH Recovery Column Simulation
Primary objective of the MEOH Recovery Column is to
recovery MEOH as a top product.
Consider the following MEOH Recovery Column to recover methanol stream as a top product.
y Feed: DME Column BTMS Stream (Refer to feedstock characterization)
1) Methanol Purity at Column Top: > 94 mole%
y MEOH Column
1) Number of Theoretical Stages: 20
3) Overall Tray Efficiencies: Can be Estimated by Correlation 4) Feed Tray Location: 11
MEOH Recovery Column Simulation
MEOH Recovery Column Simulation Continued Continued
Slide 23
Selection of appropriate thermodynamic model for the
simulation of MEOH Recovery Column is very important.
y NRTL (Non Random Two Liquid) activity coefficient
model was chosen to explain non-ideal phase behavior of liquid mixture between H2O, DME, methanol and
MEA.
y Henry’s law option was also used for the calculation of noncondensible supercritical gases in a mixed solvent.
MEOH Recovery Column Simulation
MEOH Recovery Column Simulation Continued Continued
11.0330 125.8043 35.136 46.9038 31.2179 3.81E-03 91.4268 1.3430 7.2264 0.0000 0.0000 6.77E-12 0.0000 0.0000 Liquid 28
42.0432 33.480 43.7177 31.9039 2.64E-16 96.1336 1.4409 2.4255 0.0000 0.0000 7.27E-12 0.0000 0.0000 Liquid 31
1.5330 89.7695 1.668 3.1860 21.8041 0.0560 26.8411 0.0000 73.1028 0.0000 0.0000 0.0000 0.0000 0.0000 Liquid 33