1. College of Chemical Engineering, Qingdao University of Science and Technology, Qingdao 266042, China 2. College of Chemical and Environmental Engineering, Shandong University of Science and Technology, Qingdao 266590, China 3. Shandong Collaborative Innovation Center of Eco-Chemical Engineering, Qingdao University of Science and Technology, Qingdao 266042, China
The traditional approach to solvent selection in the extractive distillation process strictly focuses on the change in the relative volatility of light-heavy components induced by the solvent. However, the total annual cost of the process may not be minimal when the solvent induces the largest change in relative volatility. This work presents a heuristic method for selecting the optimal solvent to minimize the total annual cost. The functional relationship between the relative volatility and the total annual cost is established, where the main factors, such as the relative volatility of the light-heavy components and the relative volatility of the heavy-component solvent, are taken into account. Binary azeotropic mixtures of methanol-toluene and methanol-acetone are separated to verify the feasibility of the model. The results show that using the solvent with the minimal two-column extractive distillation index, the process achieves a minimal total annual cost. The method is conducive for sustainable advancements in chemistry and engineering because a suitable solvent can be selected without simulation verification.
. [J]. Frontiers of Chemical Science and Engineering, 2020, 14(5): 824-833.
Zhaoyou Zhu, Guoxuan Li, Yao Dai, Peizhe Cui, Dongmei Xu, Yinglong Wang. Determination of a suitable index for a solvent via two-column extractive distillation using a heuristic method. Front. Chem. Sci. Eng., 2020, 14(5): 824-833.
Column diameter (D) = Aspen tray sizing Column length (L) = NT trays with 2 ft spacing plus 20% extra length Investment cost= 17640D1.066L0.802, where D and L are in m
Condensers
Heat transfer coefficient= 0.852 kW·K–1·m–2 Differential temperature= log-mean temperature difference of inlet and outlet temperature differences Investment cost= 7296A0.65, where A is in m2
TAC = (investment cost/payback period) + operating cost Plant life time= 3 years
Tab.3
Fig.3
Items
amethanol/toluene
atoluene/solvent
TAC
V
TEDI
NMP
4.23
14.90
824460.16
1.043351
0.56
Aniline
4.43
9.06
828002.21
1.008514
0.58
DMF
4.77
4.75
843445.78
1.212562
0.79
Styrene
9.20
2.61
939497.53
1.281028
1.62
o-xylene
8.82
2.54
984488.71
1.334695
1.74
p-xylene
8.78
2.15
1127997.47
1.493167
2.75
m-xylene
8.11
2.14
1359092.84
1.469316
2.81
Tab.4
Fig.4
Items
Boiling point /°C
aacetone/methanol
amethanol/solvent
Acetone
56.53
–
–
Methanol
64.7
–
–
MEA
170.8
3.001
48.253
DMSO
189
2.275
71.686
Water
100
1.915
3.772
DMF
152.8
1.640
17.790
Ethanol
78
1.622
1.780
Tab.5
Items
Boiling point /°C
aacetone/methanol
amethanol/solvent
TEDI
TAC
MEA
170
3.001
48.253
1.06
726158
DMSO
189
2.275
71.68576
2.21
915460
Water
100
1.915
3.772
4.50
1248872
DMF
152
1.64
17.79
7.32
1851981
Ethanol
78
1.622
1.78
12.77
3675550
Tab.6
Fig.5
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