变压精馏分离乙酸甲酯-甲醇-乙酸乙酯体系的设计与控制

doi:10.16085/j.issn.1000-6613.2021-2059

摘要/Abstract

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5.6×10⁵USD/a和5.7×10⁵USD/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。

关键词: 变压精馏, 动态仿真, 优化设计, 乙酸甲酯-甲醇-乙酸乙酯, 共沸物

Abstract:

The methyl acetate-methanol-ethyl acetate azeotropic mixtures can be produced in the production process of polypropylene alcohol, which must be treated immediately to avoid the environmental pollution and resource waste. In this paper, two pressure-swing distillation (PSD) separation sequences with different product orders were designed for the separation of methyl acetate-methanol-ethyl acetate mixture, which were economically optimized to obtain the optimal design parameters with the minimal total annual costs as target using genetic algorithm. The results showed that the equipment investment costs were 5.6×10⁵USD/a and 5.7×10⁵USD/a, and the energy costs were 8.8×10⁵USD/a and 1.0×10⁶USD/a for two PSD separation sequences, respectively. In addition, the control structures of the PSD scheme with economic advantages were constructed, so that the PSD process could remain stable and the purities of the three products after stabilization could still maintain near the initial set values in the face of feed flowrates and compositions disturbances.

Key words: pressure-swing distillation, dynamic simulation, optimal design, methyl acetate-methanol-ethyl acetate, azeotrope

中图分类号:

TQ021.8

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.

图/表 19

图1 常压下实验数据与不同热力学物性方法预测数据的比较

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^［24］	0.465	2.15	0.466	2.36	0.452	0.66
5.86	0.515^［24］	0.511	0.78	0.512	0.59	0.499	3.11
1.013	0.661^［25］	0.668	1.05	0.671	1.49	0.666	0.75
0.799	0.675^［25］	0.685	1.46	0.689	2.03	0.684	1.33
0.667	0.691^［25］	0.697	0.86	0.701	1.43	0.697	0.87
			Δ $X ˉ$ ₁=1.26		Δ $X ˉ$ ₂=1.58		Δ $X ˉ$ ₃=1.34

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^［24］	0.465	2.15	0.466	2.36	0.452	0.66
5.86	0.515^［24］	0.511	0.78	0.512	0.59	0.499	3.11
1.013	0.661^［25］	0.668	1.05	0.671	1.49	0.666	0.75
0.799	0.675^［25］	0.685	1.46	0.689	2.03	0.684	1.33
0.667	0.691^［25］	0.697	0.86	0.701	1.43	0.697	0.87
			Δ $X ˉ$ ₁=1.26		Δ $X ˉ$ ₂=1.58		Δ $X ˉ$ ₃=1.34

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^［26］	0.723	2.56	0.727	2.02	0.722	2.70
1.013	0.700^［27］	0.703	0.43	0.708	1.14	0.703	0.43
0.92	0.698^［27］	0.698	0	0.702	0.57	0.698	0
			Δ $X ˉ$ ₁=1.00		Δ $X ˉ$ ₂=1.24		Δ $X ˉ$ ₃=1.04

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^［26］	0.723	2.56	0.727	2.02	0.722	2.70
1.013	0.700^［27］	0.703	0.43	0.708	1.14	0.703	0.43
0.92	0.698^［27］	0.698	0	0.702	0.57	0.698	0
			Δ $X ˉ$ ₁=1.00		Δ $X ˉ$ ₂=1.24		Δ $X ˉ$ ₃=1.04

图2 常压下MA-MET-EA的三元相图

图3 不同压力下MET-MA体系T-X-Y图

图4 两种变压精馏流程

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

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

图5 遗传算法程序

图6 优化后两种变压精馏分离序列

图7 温度灵敏板的判别

图8 控制结构Ⅰ

图9 控制结构Ⅰ的动态响应

图10 控制结构Ⅱ

图11 控制结构Ⅱ的动态响应

图12 控制结构Ⅲ

图13 控制结构Ⅲ的动态响应

图14 控制结构Ⅳ

图15 控制结构Ⅳ的动态响应

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