CIESC Journal ›› 2022, Vol. 73 ›› Issue (1): 322-331.DOI: 10.11949/0438-1157.20211441
• Separation engineering • Previous Articles Next Articles
Zixuan HUANG1(),Huan CHEN1(),Hai LI1,2(),Minglong WANG1,Guangjin CHEN1,Bei LIU1
Received:
2021-10-09
Revised:
2021-11-27
Online:
2022-01-18
Published:
2022-01-05
Contact:
Hai LI
黄子轩1(),陈欢1(),李海1,2(),王明龙1,陈光进1,刘蓓1
通讯作者:
李海
作者简介:
黄子轩(1996—),男,博士研究生,基金资助:
CLC Number:
Zixuan HUANG, Huan CHEN, Hai LI, Minglong WANG, Guangjin CHEN, Bei LIU. Process simulation and energy consumption analysis of CO2/N2 pilot-scale separation using ZIF-8 slurry[J]. CIESC Journal, 2022, 73(1): 322-331.
黄子轩, 陈欢, 李海, 王明龙, 陈光进, 刘蓓. ZIF-8浆液中试分离CO2/N2过程模拟及能耗分析[J]. 化工学报, 2022, 73(1): 322-331.
Fig.4 Computation module of Wcompr: gas compression module in the Aspen Plus (COMPR); gas stream before compression (FEED-GAS); gas stream after compression (COMP-GAS)
Fig.5 Computation module of Wmet: metering pump module in the Aspen Plus (MET-PUMP); lean slurry under desorption pressure (SLU-IN); lean slurry under sorption pressure (SLU-OUT)
Fig.6 Computation module of Wvac: vacuum pump module in the Aspen Plus (VACUUM); gas stream under normal pressure (DE); gas stream under desorption pressure (NOL)
Fig.7 Computation module of Qheat: heat exchanger module in the Aspen Plus (HEATX); lean slurry from desorption tower to heat exchanger (LEAN-IN); lean slurry from heat exchanger to sorption tower (LEAN-OUT); rich slurry from the sorption tower to heat exchanger (RICH-IN); rich slurry from heat exchanger to heater (RICH-OUT); rich slurry from heater to desorption tower (RICH)
Fig.8 Sorption isotherms of CO2 at 303.15 K in fresh ZIF-8 slurry (a), the ZIF-8 slurry obtained from the desorption packed tower(desorption condition: the desorption temperature, pressure, and air-purge flow rate were fixed at 333.15 K, 0.08 MPa, and 200 L/h)(b); Sorption isotherm of N2 at 303.15 K in fresh ZIF-8 slurry (c)[33]
ZIF-8浆液 | kCO2=(mT+n)p+MT+N | |||
---|---|---|---|---|
m | n | M | N | |
新鲜ZIF-8浆液 | -0.01148 | 4.20695 | 0.00029 | -0.54962 |
从中试解吸塔底获得的ZIF-8浆液① | -0.01776 | 5.82127 | 0.00156 | -0.88403 |
Table 1 The relationship between temperature, pressure, and the binary interaction parameter kCO2 of CO2 and ZIF-8 slurry
ZIF-8浆液 | kCO2=(mT+n)p+MT+N | |||
---|---|---|---|---|
m | n | M | N | |
新鲜ZIF-8浆液 | -0.01148 | 4.20695 | 0.00029 | -0.54962 |
从中试解吸塔底获得的ZIF-8浆液① | -0.01776 | 5.82127 | 0.00156 | -0.88403 |
T/K | kCO2 | pE/MPa | xcal | xexp | AADx/% |
---|---|---|---|---|---|
293.15 | -0.4596 | 0.007 | 0.0067 | 0.0078 | 13.40 |
293.15 | -0.4503 | 0.018 | 0.0145 | 0.0137 | 5.24 |
293.15 | -0.4352 | 0.036 | 0.0223 | 0.0203 | 9.66 |
293.15 | -0.4032 | 0.074 | 0.0281 | 0.0265 | 6.15 |
303.15 | -0.4575 | 0.007 | 0.0046 | 0.0054 | 13.52 |
303.15 | -0.4495 | 0.018 | 0.0104 | 0.0103 | 0.55 |
303.15 | -0.4292 | 0.046 | 0.0191 | 0.0179 | 6.82 |
303.15 | -0.4045 | 0.08 | 0.0233 | 0.0230 | 1.30 |
303.15 | -0.3870 | 0.104 | 0.0237 | 0.0262 | 9.40 |
313.15 | -0.4530 | 0.011 | 0.0050 | 0.0050 | 1.15 |
313.15 | -0.4444 | 0.025 | 0.0098 | 0.0098 | 0.18 |
313.15 | -0.4334 | 0.043 | 0.0143 | 0.0144 | 0.75 |
313.15 | -0.4114 | 0.079 | 0.0193 | 0.0187 | 3.01 |
313.15 | -0.3906 | 0.113 | 0.0209 | 0.0215 | 3.03 |
总AADx | 5.30 |
Table 2 Experimental and simulated phase equilibrium data of CO2 absorption by fresh ZIF-8 slurry
T/K | kCO2 | pE/MPa | xcal | xexp | AADx/% |
---|---|---|---|---|---|
293.15 | -0.4596 | 0.007 | 0.0067 | 0.0078 | 13.40 |
293.15 | -0.4503 | 0.018 | 0.0145 | 0.0137 | 5.24 |
293.15 | -0.4352 | 0.036 | 0.0223 | 0.0203 | 9.66 |
293.15 | -0.4032 | 0.074 | 0.0281 | 0.0265 | 6.15 |
303.15 | -0.4575 | 0.007 | 0.0046 | 0.0054 | 13.52 |
303.15 | -0.4495 | 0.018 | 0.0104 | 0.0103 | 0.55 |
303.15 | -0.4292 | 0.046 | 0.0191 | 0.0179 | 6.82 |
303.15 | -0.4045 | 0.08 | 0.0233 | 0.0230 | 1.30 |
303.15 | -0.3870 | 0.104 | 0.0237 | 0.0262 | 9.40 |
313.15 | -0.4530 | 0.011 | 0.0050 | 0.0050 | 1.15 |
313.15 | -0.4444 | 0.025 | 0.0098 | 0.0098 | 0.18 |
313.15 | -0.4334 | 0.043 | 0.0143 | 0.0144 | 0.75 |
313.15 | -0.4114 | 0.079 | 0.0193 | 0.0187 | 3.01 |
313.15 | -0.3906 | 0.113 | 0.0209 | 0.0215 | 3.03 |
总AADx | 5.30 |
T/K | kCO2 | pE/MPa | xcal | xexp | AADx/% |
---|---|---|---|---|---|
293.15 | -0.4224 | 0.007 | 0.0039 | 0.0044 | 12.75 |
293.15 | -0.4113 | 0.025 | 0.0113 | 0.0096 | 17.46 |
293.15 | -0.3990 | 0.045 | 0.0166 | 0.0154 | 8.32 |
293.15 | -0.3751 | 0.084 | 0.0215 | 0.0207 | 3.65 |
293.15 | -0.3615 | 0.106 | 0.0222 | 0.0227 | 2.38 |
303.15 | -0.4067 | 0.01 | 0.0032 | 0.0035 | 7.90 |
303.15 | -0.3997 | 0.026 | 0.0074 | 0.0072 | 1.95 |
303.15 | -0.3932 | 0.041 | 0.0105 | 0.0112 | 5.88 |
303.15 | -0.3809 | 0.069 | 0.0147 | 0.0157 | 6.37 |
303.15 | -0.3648 | 0.106 | 0.0179 | 0.0190 | 5.77 |
313.15 | -0.3911 | 0.017 | 0.0033 | 0.0033 | 1.10 |
313.15 | -0.3875 | 0.031 | 0.0057 | 0.0054 | 4.66 |
313.15 | -0.3838 | 0.045 | 0.0078 | 0.0076 | 2.91 |
313.15 | -0.3797 | 0.061 | 0.0099 | 0.0098 | 1.65 |
313.15 | -0.3724 | 0.089 | 0.0131 | 0.0127 | 3.19 |
313.15 | -0.3690 | 0.102 | 0.0143 | 0.0141 | 1.56 |
总AADx | 5.47 |
Table 3 Experimental and simulated phase equilibrium data of CO2 absorption by ZIF-8 slurry obtained from the desorption packed tower
T/K | kCO2 | pE/MPa | xcal | xexp | AADx/% |
---|---|---|---|---|---|
293.15 | -0.4224 | 0.007 | 0.0039 | 0.0044 | 12.75 |
293.15 | -0.4113 | 0.025 | 0.0113 | 0.0096 | 17.46 |
293.15 | -0.3990 | 0.045 | 0.0166 | 0.0154 | 8.32 |
293.15 | -0.3751 | 0.084 | 0.0215 | 0.0207 | 3.65 |
293.15 | -0.3615 | 0.106 | 0.0222 | 0.0227 | 2.38 |
303.15 | -0.4067 | 0.01 | 0.0032 | 0.0035 | 7.90 |
303.15 | -0.3997 | 0.026 | 0.0074 | 0.0072 | 1.95 |
303.15 | -0.3932 | 0.041 | 0.0105 | 0.0112 | 5.88 |
303.15 | -0.3809 | 0.069 | 0.0147 | 0.0157 | 6.37 |
303.15 | -0.3648 | 0.106 | 0.0179 | 0.0190 | 5.77 |
313.15 | -0.3911 | 0.017 | 0.0033 | 0.0033 | 1.10 |
313.15 | -0.3875 | 0.031 | 0.0057 | 0.0054 | 4.66 |
313.15 | -0.3838 | 0.045 | 0.0078 | 0.0076 | 2.91 |
313.15 | -0.3797 | 0.061 | 0.0099 | 0.0098 | 1.65 |
313.15 | -0.3724 | 0.089 | 0.0131 | 0.0127 | 3.19 |
313.15 | -0.3690 | 0.102 | 0.0143 | 0.0141 | 1.56 |
总AADx | 5.47 |
Fig.10 Sorption heat of ZIF-8 slurry in fresh ZIF-8 slurry (a) and the ZIF-8 slurry obtained from the desorption packed tower (the desorption temperature, pressure, and air-purge flow rate were fixed at 333.15 K, 0.08 MPa, and 200 L/h) (b)
理论塔板级数 | 气相中CO2浓度,y/% | 液相中CO2浓度,x/% | 气相中CO2分压,p/MPa | 平衡级温度,T/K | CO2-浆液二元交互作用参数,kCO2 |
---|---|---|---|---|---|
塔顶(净化气/贫液) | 0 | 0 | 0 | 303.15 | -0.4626 |
2 | 0.0001 | 0 | 0 | 303.15 | -0.4626 |
3 | 0.0005 | 0 | 0 | 303.15 | -0.4626 |
4 | 0.0034 | 0.0002 | 0 | 303.15 | -0.4626 |
5 | 0.0235 | 0.0015 | 0.0001 | 303.16 | -0.4625 |
6 | 0.1612 | 0.0105 | 0.001 | 303.22 | -0.4619 |
7 | 1.078 | 0.0706 | 0.0065 | 303.6 | -0.4578 |
8 | 6.2328 | 0.4297 | 0.0374 | 305.9 | -0.4358 |
塔底(原料气/富液) | 20 | 1.5859 | 0.12 | 313.3 | -0.3865 |
Table 4 The simulation results of multi-stage CO2 absorption by fresh ZIF-8 slurry
理论塔板级数 | 气相中CO2浓度,y/% | 液相中CO2浓度,x/% | 气相中CO2分压,p/MPa | 平衡级温度,T/K | CO2-浆液二元交互作用参数,kCO2 |
---|---|---|---|---|---|
塔顶(净化气/贫液) | 0 | 0 | 0 | 303.15 | -0.4626 |
2 | 0.0001 | 0 | 0 | 303.15 | -0.4626 |
3 | 0.0005 | 0 | 0 | 303.15 | -0.4626 |
4 | 0.0034 | 0.0002 | 0 | 303.15 | -0.4626 |
5 | 0.0235 | 0.0015 | 0.0001 | 303.16 | -0.4625 |
6 | 0.1612 | 0.0105 | 0.001 | 303.22 | -0.4619 |
7 | 1.078 | 0.0706 | 0.0065 | 303.6 | -0.4578 |
8 | 6.2328 | 0.4297 | 0.0374 | 305.9 | -0.4358 |
塔底(原料气/富液) | 20 | 1.5859 | 0.12 | 313.3 | -0.3865 |
理论塔板级数 | 气相中CO2浓度,y/% | 液相中CO2浓度,x/% | 气相中CO2分压,p/MPa | 平衡级温度,T/K | CO2-浆液二元交互作用参数,kCO2 |
---|---|---|---|---|---|
塔顶(净化气/贫液) | 0.0429 | 0 | 0.0003 | 303.15 | -0.411 |
2 | 0.1794 | 0.0089 | 0.0011 | 303.2 | -0.4106 |
3 | 0.6083 | 0.0369 | 0.0036 | 303.38 | -0.4092 |
4 | 1.894 | 0.1223 | 0.0114 | 303.93 | -0.4051 |
5 | 5.2582 | 0.3561 | 0.0315 | 305.42 | -0.395 |
6 | 11.503 | 0.8351 | 0.069 | 308.49 | -0.3791 |
7 | 17.4369 | 1.3552 | 0.1046 | 311.81 | -0.3679 |
8 | 19.5741 | 1.5612 | 0.1174 | 313.13 | -0.365 |
塔底(原料气/富液) | 20 | 1.5832 | 0.12 | 313.27 | -0.3644 |
Table 5 The simulation results of multi-stage CO2 absorption by ZIF-8 slurry obtained from the desorption packed tower
理论塔板级数 | 气相中CO2浓度,y/% | 液相中CO2浓度,x/% | 气相中CO2分压,p/MPa | 平衡级温度,T/K | CO2-浆液二元交互作用参数,kCO2 |
---|---|---|---|---|---|
塔顶(净化气/贫液) | 0.0429 | 0 | 0.0003 | 303.15 | -0.411 |
2 | 0.1794 | 0.0089 | 0.0011 | 303.2 | -0.4106 |
3 | 0.6083 | 0.0369 | 0.0036 | 303.38 | -0.4092 |
4 | 1.894 | 0.1223 | 0.0114 | 303.93 | -0.4051 |
5 | 5.2582 | 0.3561 | 0.0315 | 305.42 | -0.395 |
6 | 11.503 | 0.8351 | 0.069 | 308.49 | -0.3791 |
7 | 17.4369 | 1.3552 | 0.1046 | 311.81 | -0.3679 |
8 | 19.5741 | 1.5612 | 0.1174 | 313.13 | -0.365 |
塔底(原料气/富液) | 20 | 1.5832 | 0.12 | 313.27 | -0.3644 |
Test No. | Tde/K | pde/MPa | Vde-air/(L/h) | pab/MPa | Vin-mixgas/(L/h) | φ | Cout-CO2/% (mol) | ΔSV/(mol/L) | ηCO2/% | wtotal/(GJ/t CO2) |
---|---|---|---|---|---|---|---|---|---|---|
S1 | 298 | 0.08 | 200 | 0.6 | 300 | 18 | 3.07 | 0.12 | 84.6 | 0.680 |
S2 | 298 | 0.08 | 600 | 0.6 | 720 | 42 | 5.82 | 0.26 | 69.1 | 0.609 |
S3 | 313 | 0.08 | 600 | 0.6 | 720 | 42 | 3.08 | 0.32 | 84.1 | 0.649 |
S4 | 333 | 0.08 | 200 | 0.6 | 720 | 90 | 1.42 | 0.75 | 93.0 | 0.507 |
S5 | 333 | 0.08 | 200 | 0.6 | 720 | 80 | 0.92 | 0.68 | 95.0 | 0.509 |
S6 | 333 | 0.08 | 200 | 0.5 | 720 | 80 | 2.02 | 0.64 | 89.9 | 0.474 |
SMEA | 333 | 0.08 | 200 | 0.6 | 720 | 90 | 3.39 | 0.66 | 82.5 | 0.957 |
Table 6 Effect of different operating conditions of ZIF-8 slurry on the CO2 capture equivalent work in the packed tower
Test No. | Tde/K | pde/MPa | Vde-air/(L/h) | pab/MPa | Vin-mixgas/(L/h) | φ | Cout-CO2/% (mol) | ΔSV/(mol/L) | ηCO2/% | wtotal/(GJ/t CO2) |
---|---|---|---|---|---|---|---|---|---|---|
S1 | 298 | 0.08 | 200 | 0.6 | 300 | 18 | 3.07 | 0.12 | 84.6 | 0.680 |
S2 | 298 | 0.08 | 600 | 0.6 | 720 | 42 | 5.82 | 0.26 | 69.1 | 0.609 |
S3 | 313 | 0.08 | 600 | 0.6 | 720 | 42 | 3.08 | 0.32 | 84.1 | 0.649 |
S4 | 333 | 0.08 | 200 | 0.6 | 720 | 90 | 1.42 | 0.75 | 93.0 | 0.507 |
S5 | 333 | 0.08 | 200 | 0.6 | 720 | 80 | 0.92 | 0.68 | 95.0 | 0.509 |
S6 | 333 | 0.08 | 200 | 0.5 | 720 | 80 | 2.02 | 0.64 | 89.9 | 0.474 |
SMEA | 333 | 0.08 | 200 | 0.6 | 720 | 90 | 3.39 | 0.66 | 82.5 | 0.957 |
Test No. | wcompr/(GJ/t CO2) | wheat/(GJ/t CO2) | wpump/(GJ/t CO2) | wtotal/(GJ/t CO2) |
---|---|---|---|---|
S1 | 0.477 | 0.000 | 0.203 | 0.680 |
S2 | 0.478 | 0.000 | 0.131 | 0.609 |
S3 | 0.412 | 0.119 | 0.117 | 0.649 |
S4 | 0.382 | 0.081 | 0.045 | 0.507 |
S5 | 0.374 | 0.084 | 0.051 | 0.509 |
S6 | 0.343 | 0.086 | 0.045 | 0.474 |
SMEA | 0.418 | 0.177 | 0.052 | 0.957 |
Table 7 The composition of CO2 capture equivalent work in different operating conditions
Test No. | wcompr/(GJ/t CO2) | wheat/(GJ/t CO2) | wpump/(GJ/t CO2) | wtotal/(GJ/t CO2) |
---|---|---|---|---|
S1 | 0.477 | 0.000 | 0.203 | 0.680 |
S2 | 0.478 | 0.000 | 0.131 | 0.609 |
S3 | 0.412 | 0.119 | 0.117 | 0.649 |
S4 | 0.382 | 0.081 | 0.045 | 0.507 |
S5 | 0.374 | 0.084 | 0.051 | 0.509 |
S6 | 0.343 | 0.086 | 0.045 | 0.474 |
SMEA | 0.418 | 0.177 | 0.052 | 0.957 |
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