化工进展 ›› 2022, Vol. 41 ›› Issue (8): 4065-4076.DOI: 10.16085/j.issn.1000-6613.2021-2059
向晟1(), 王超1, 庄钰1, 顾偲雯1,2, 张磊1(), 都健1
收稿日期:
2021-09-30
修回日期:
2021-12-14
出版日期:
2022-08-25
发布日期:
2022-08-22
通讯作者:
张磊
作者简介:
向晟(1998—),男,硕士研究生,研究方向为化工过程与产品设计。E-mail:基金资助:
XIANG Sheng1(), WANG Chao1, ZHUANG Yu1, GU Siwen1,2, ZHANG Lei1(), DU Jian1
Received:
2021-09-30
Revised:
2021-12-14
Online:
2022-08-25
Published:
2022-08-22
Contact:
ZHANG Lei
摘要:
聚丙烯醇的生产过程会产生乙酸甲酯-甲醇-乙酸乙酯共沸混合物,如果不及时处理,必然会造成环境污染和资源浪费。本文采用变压精馏的方式,针对乙酸甲酯-甲醇-乙酸乙酯体系设计了两种产品顺序不同的变压精馏分离序列,并采用遗传算法以年度总费用最小为目标,对两种分离序列进行优化设计以获得最优的设计参数。优化结果表明,两种变压精馏分离方案的设备投资费用分别为5.6×105 USD/a和5.7×105 USD/a,能耗费用分别为8.8×105USD/a和1.0×106USD/a。此外,对具有经济优势的变压精馏分离方案进行了控制结构的构建,使该过程在面对进料流量扰动和进料组分扰动时仍能维持稳定,稳定之后的三种产品纯度仍能维持在设定值附近。
中图分类号:
向晟, 王超, 庄钰, 顾偲雯, 张磊, 都健. 变压精馏分离乙酸甲酯-甲醇-乙酸乙酯体系的设计与控制[J]. 化工进展, 2022, 41(8): 4065-4076.
XIANG Sheng, WANG Chao, ZHUANG Yu, GU Siwen, ZHANG Lei, DU Jian. Design and control of pressure-swing distillation for separating methyl acetate-methanol-ethyl acetate azeotropic system[J]. Chemical Industry and Engineering Progress, 2022, 41(8): 4065-4076.
压力/bar | X实验 | X预测1 | ΔX1/% | X预测2 | ΔX2/% | X预测3 | ΔX3/% |
---|---|---|---|---|---|---|---|
8.77 | 0.455[ | 0.465 | 2.15 | 0.466 | 2.36 | 0.452 | 0.66 |
5.86 | 0.515[ | 0.511 | 0.78 | 0.512 | 0.59 | 0.499 | 3.11 |
1.013 | 0.661[ | 0.668 | 1.05 | 0.671 | 1.49 | 0.666 | 0.75 |
0.799 | 0.675[ | 0.685 | 1.46 | 0.689 | 2.03 | 0.684 | 1.33 |
0.667 | 0.691[ | 0.697 | 0.86 | 0.701 | 1.43 | 0.697 | 0.87 |
Δ | Δ | Δ |
表1 不同压力下乙酸甲酯-甲醇(MA-MET)体系共沸组成实验值与预测值比较
压力/bar | X实验 | X预测1 | ΔX1/% | X预测2 | ΔX2/% | X预测3 | ΔX3/% |
---|---|---|---|---|---|---|---|
8.77 | 0.455[ | 0.465 | 2.15 | 0.466 | 2.36 | 0.452 | 0.66 |
5.86 | 0.515[ | 0.511 | 0.78 | 0.512 | 0.59 | 0.499 | 3.11 |
1.013 | 0.661[ | 0.668 | 1.05 | 0.671 | 1.49 | 0.666 | 0.75 |
0.799 | 0.675[ | 0.685 | 1.46 | 0.689 | 2.03 | 0.684 | 1.33 |
0.667 | 0.691[ | 0.697 | 0.86 | 0.701 | 1.43 | 0.697 | 0.87 |
Δ | Δ | Δ |
压力/bar | X实验 | X预测1 | ΔX1/% | X预测2 | ΔX2/% | X预测3 | ΔX3/% |
---|---|---|---|---|---|---|---|
1.41 | 0.742[ | 0.723 | 2.56 | 0.727 | 2.02 | 0.722 | 2.70 |
1.013 | 0.700[ | 0.703 | 0.43 | 0.708 | 1.14 | 0.703 | 0.43 |
0.92 | 0.698[ | 0.698 | 0 | 0.702 | 0.57 | 0.698 | 0 |
Δ | Δ | Δ |
表2 不同压力下甲醇-乙酸乙酯(MET-EA)体系共沸组成实验值与预测值比较
压力/bar | X实验 | X预测1 | ΔX1/% | X预测2 | ΔX2/% | X预测3 | ΔX3/% |
---|---|---|---|---|---|---|---|
1.41 | 0.742[ | 0.723 | 2.56 | 0.727 | 2.02 | 0.722 | 2.70 |
1.013 | 0.700[ | 0.703 | 0.43 | 0.708 | 1.14 | 0.703 | 0.43 |
0.92 | 0.698[ | 0.698 | 0 | 0.702 | 0.57 | 0.698 | 0 |
Δ | Δ | Δ |
压力范围/bar | 系数C的取值 |
---|---|
0~3.4 | 3919.32 |
3.4~6.8 | 3966.20 |
6.8~13.6 | 4059.96 |
13.6~20.5 | 4106.85 |
表3 不同压力范围下的系数C的取值
压力范围/bar | 系数C的取值 |
---|---|
0~3.4 | 3919.32 |
3.4~6.8 | 3966.20 |
6.8~13.6 | 4059.96 |
13.6~20.5 | 4106.85 |
蒸汽类型 | 压力/bar | 温度/℃ | 价格/USD·kJ-1 |
---|---|---|---|
低压蒸汽 | 6 | 160 | 7.78×10-6 |
中压蒸汽 | 11 | 184 | 8.22×10-6 |
高压蒸汽 | 42 | 254 | 9.88×10-6 |
表4 不同压力的加热蒸汽价格
蒸汽类型 | 压力/bar | 温度/℃ | 价格/USD·kJ-1 |
---|---|---|---|
低压蒸汽 | 6 | 160 | 7.78×10-6 |
中压蒸汽 | 11 | 184 | 8.22×10-6 |
高压蒸汽 | 42 | 254 | 9.88×10-6 |
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