反应精馏合成乙酸异丙酯过程的强化与动态控制
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摘要
为了解决传统反应精馏难以得到高纯度乙酸异丙酯的难题,将反应精馏与萃取精馏工艺耦合在一个塔中,打破产物间的共沸,得到高纯度的乙酸异丙酯。同时采用萃取剂循环物流对异丙醇进行预热,以降低反应萃取精馏塔的再沸器热负荷。利用Aspen Plus模拟软件对该流程模拟,得到乙酸异丙酯的摩尔分数可达99.5%,在此基础上以年度总费用(TAC)最小为优化目标,得到最优的操作参数。基于经济最优流程,对反应萃取精馏合成乙酸异丙酯流程进行控制结构的设计,采用相对增益矩阵(RGA)判据获得不同的操纵变量与控制变量匹配关系,提出了3种动态控制结构并对其动态特性进行了分析。结果表明,Q/F-温度串级控制结构可有效抵抗扰动,稳定后产品纯度偏差较小,且回稳时间相比温差控制更短,可以保证生产的平稳运行。
Often the conventional reactive distillation column cannot produce high purity isopropyl acetate(IPAc).In this work, the reactive distillation and extractive distillation were integrated into one column to obtain high purity IPAc, and the inlet isopropanol was preheated to reduce the reboiler heat load of reactive and extractive distillation column. Subsequently, the process was simulated by the Aspen Plus software, and the results show that the molar fraction of IPAc reaches 99.5%. The optimal operating conditions are obtained with the minimum total annual cost(TAC) as the target function. Based on the steady-state simulation design data, the control structures were designed for reactive and extractive distillation processes. Different matching relationships between manipulate and control variables are determined through the relative gain array(RGA) criterion, and the dynamic characteristics of three control structures were analyzed. The results indicate that the Q/F-temperature cascade control has a shorter settling time and less purity deviation than the temperature difference control structure, which can handle the disturbances effectively and keep the process running smoothly.
Often the conventional reactive distillation column cannot produce high purity isopropyl acetate(IPAc).In this work, the reactive distillation and extractive distillation were integrated into one column to obtain high purity IPAc, and the inlet isopropanol was preheated to reduce the reboiler heat load of reactive and extractive distillation column. Subsequently, the process was simulated by the Aspen Plus software, and the results show that the molar fraction of IPAc reaches 99.5%. The optimal operating conditions are obtained with the minimum total annual cost(TAC) as the target function. Based on the steady-state simulation design data, the control structures were designed for reactive and extractive distillation processes. Different matching relationships between manipulate and control variables are determined through the relative gain array(RGA) criterion, and the dynamic characteristics of three control structures were analyzed. The results indicate that the Q/F-temperature cascade control has a shorter settling time and less purity deviation than the temperature difference control structure, which can handle the disturbances effectively and keep the process running smoothly.
引文
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[13]冯加双.正丙醇与乙酸甲酯的酯交换反应的反应精馏过程设计[D].北京:北京化工大学,2017.
[14]李洪,孟莹,李鑫钢,等.乙酸戊酯酯化反应精馏过程系统控制模拟及分析[J].化工进展,2015,34(12):4165-4171.(LI Hong,MENG Ying,LI Xingang,et al.Dynamic simulation and analysis of reactive distillation column for production of amyl acetate[J].Chemical Industry and Engineering Progress,2015,34(12):4165-4171.)
[15]GAO X,WANG F,LI H,et al.Heat-integrated reactive distillation process for TAME synthesis[J].Separation&Purification Technology,2014,132:468-478.
[16]孔沙沙.催化精馏合成乙酸异丙酯新工艺研究[D].烟台:烟台大学,2014.
[17]TANG Y T,CHEN Y W,HUANG H P,et al.Design of reactive distillations for acetic acid esterification[J].AICHE Journal,2005,51(6):1683-1699.
[18]DOUGLAS J M.Conceptual Design of Chemical Processes[M].New York:McGraw-Hill,1988:568-577.
[19]李宏熙.乙二醇单丁醚反应精馏塔控制方案设计及分析[D].青岛:中国海洋大学,2013.
[20]LUYBEN W L.Distillation Design and Control Using AspenTMSimulation[M].New York:John Wiley&Sons,2013:171-174
[21]WEI C,HUANG K,CHEN H,et al.Design and operation of dividing-wall distillation columns.1.Diminishing the black-hole problem through over-design[J].Chemical Engineering&Processing Process Intensification,2014,75(1):90-109.
[22]WU N,HUANG K,LUAN S.Operation of dividingwall distillation columns.2.A double temperature difference controlscheme[J].Industrial&Engineering Chemistry Research,2013,52(15):5365-5383.
[23]YANG Y,HUANG K.Operation of dividing-wall distillation columns.3.A simplified double temperature difference controlscheme[J].Industrial&Engineering Chemistry Research,2014,53(41):15969-15979.
[2]徐红,魏巍,虞昊,等.反应精馏合成丙酸丙酯模拟与动力学[J].石油学报(石油加工),2015,31(6):1363-1369.(XU Hong,WEI Wei,YU Hao,et al.Simulation and reaction kinetics of synthesis of propyl propionate by reactive distillation[J].Acta Petrolei Sinica(Petroleum Processing Section),2015,31(6):1363-1369.
[3]CHO M,HAN M.Dynamics and control of entrainer enhanced reactive distillation using an extraneous entrainer for the production of butyl acetate[J].Journal of Process Control,2018,61:58-76.
[4]ZHANG Q,GUO T,YU C,et al.Design and control of different pressure thermally coupled reactive distillation for amyl acetate synthesis[J].Chemical Engineering&Processing Process Intensification,2017,121:170-179.
[5]高鑫,赵悦,李洪,等.反应精馏过程耦合强化技术基础与应用研究述评[J].化工学报,2018,69(1):218-238.(GAO Xin,ZHAO Yue,LI Hong,et al.Review of basic and application investigation of reactive distillation technology for process intensification[J].CIESC Journal,2018,69(1):218-238.)
[6]ZHANG B,YANG W,HU S,et al.A reactive distillation process with a sidedraw stream to enhance the production of isopropyl acetate[J].Chemical Engineering&Processing Process Intensification,2013,70(3):117-130.
[7]LEE H,LAI I,HUANG H,et al.Design and control of thermally coupled reactive distillation for the production of isopropyl acetate[J].Industrial&Engineering Chemistry Research,2012,51(36):11753-11763.
[8]ZHAO T,LI J,ZHOU H,et al.A thermally coupled reactive distillation process to intensify the synthesis of isopropyl acetate[J].Chemical Engineering&Processing Process Intensification,2018,124:97-108.
[9]QI W,MALONE M.Semibatch reactive distillation for isopropyl acetate synthesis[J].Industrial&Engineering Chemistry Research,2010,50(3):1272-1277.
[10]LAI I,HUNG S,HUNG W,et al.Design and control of reactive distillation for ethyl and isopropyl acetates production withazeotropic feeds[J].Chemical Engineering Science,2007,62(3):878-898.
[11]金浩,陆佳伟,汤吉海.带侧线反应精馏-渗透汽化生产乙酸乙酯集成过程模拟与分析[J].化工学报,2018,69(8):3469-3478.(JIN Hao,LU Jiawei,TANGJihai.Simulation and analysis of a side stream reactive distillation-pervaporation integrated process for ethyl acetate production[J].CIESC Journal,2018,69(8):3469-3478.)
[12]CAI J,CUI X,YANG Z.Simulation for transesterification of methyl acetate and n-butanol in a reactive and extractive distillation column using ionic liquids as entrainer and catalyst[J].Chinese Journal of Chemical Engineering,2011,19(5):754-762.
[13]冯加双.正丙醇与乙酸甲酯的酯交换反应的反应精馏过程设计[D].北京:北京化工大学,2017.
[14]李洪,孟莹,李鑫钢,等.乙酸戊酯酯化反应精馏过程系统控制模拟及分析[J].化工进展,2015,34(12):4165-4171.(LI Hong,MENG Ying,LI Xingang,et al.Dynamic simulation and analysis of reactive distillation column for production of amyl acetate[J].Chemical Industry and Engineering Progress,2015,34(12):4165-4171.)
[15]GAO X,WANG F,LI H,et al.Heat-integrated reactive distillation process for TAME synthesis[J].Separation&Purification Technology,2014,132:468-478.
[16]孔沙沙.催化精馏合成乙酸异丙酯新工艺研究[D].烟台:烟台大学,2014.
[17]TANG Y T,CHEN Y W,HUANG H P,et al.Design of reactive distillations for acetic acid esterification[J].AICHE Journal,2005,51(6):1683-1699.
[18]DOUGLAS J M.Conceptual Design of Chemical Processes[M].New York:McGraw-Hill,1988:568-577.
[19]李宏熙.乙二醇单丁醚反应精馏塔控制方案设计及分析[D].青岛:中国海洋大学,2013.
[20]LUYBEN W L.Distillation Design and Control Using AspenTMSimulation[M].New York:John Wiley&Sons,2013:171-174
[21]WEI C,HUANG K,CHEN H,et al.Design and operation of dividing-wall distillation columns.1.Diminishing the black-hole problem through over-design[J].Chemical Engineering&Processing Process Intensification,2014,75(1):90-109.
[22]WU N,HUANG K,LUAN S.Operation of dividingwall distillation columns.2.A double temperature difference controlscheme[J].Industrial&Engineering Chemistry Research,2013,52(15):5365-5383.
[23]YANG Y,HUANG K.Operation of dividing-wall distillation columns.3.A simplified double temperature difference controlscheme[J].Industrial&Engineering Chemistry Research,2014,53(41):15969-15979.