双溶剂协同萃取精馏分离乙酸甲酯-甲醇-水工艺模拟
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摘要
针对乙酸甲酯-甲醇-水体系,在筛选萃取剂的基础上,提出了双溶剂四塔萃取精馏、单溶剂三塔萃取精馏及双溶剂协同萃取精馏3种分离工艺.用Aspen Plus软件模拟萃取精馏过程,并以能耗和年总费用作为评价指标,用SR-Polar方程计算各萃取精馏工艺合适的操作参数和设备参数.结果表明,水和乙二醇是分离该体系较合适的萃取剂,单溶剂三塔萃取精馏工艺较双溶剂四塔萃取精馏工艺优异,能耗减少约37.9%,年总费用降低约38.9%.双溶剂协同萃取精馏工艺比双溶剂四塔萃取精馏工艺和单溶剂三塔萃取精馏工艺能耗分别减少约45.6%和12.4%,年总费用分别降低约43.5%和11.6%.
According to the characteristic of methyl acetate-methanol-water system in the presence of two kinds of azeotrope, three separation processes such as double solvent four column extractive distillation process, single solvent three column extractive distillation process and double solvent synergistic extractive distillation process were proposed on the basis of screening the extraction agent for the system. Energy consumption and total annual cost(TAC) as evaluation index, the simulations for the three separation processes were performed by Aspen Plus software which SR-Polar thermodynamic model was used to calculate phase equilibrium data and Rad Frac model was used to simulate distillation column, and the optimal operating parameters and equipment parameters for the three separation processes were obtained. Simulation results showed that water and ethylene glycol were suitable extractants for the separation system, the single solvent three column extractive distillation process was better than the double solvent four column extractive distillation process and the energy consumption could be reduced by 37.9%, TAC decreased by 38.9%. Compared with the double solvent four column extractive distillation process and single solvent three column extractive distillation process, the double solvent synergistic extractive distillation process can save energy by 45.6% and 12.4%, reduce TAC by 43.5% and 11.6%, respectively.
According to the characteristic of methyl acetate-methanol-water system in the presence of two kinds of azeotrope, three separation processes such as double solvent four column extractive distillation process, single solvent three column extractive distillation process and double solvent synergistic extractive distillation process were proposed on the basis of screening the extraction agent for the system. Energy consumption and total annual cost(TAC) as evaluation index, the simulations for the three separation processes were performed by Aspen Plus software which SR-Polar thermodynamic model was used to calculate phase equilibrium data and Rad Frac model was used to simulate distillation column, and the optimal operating parameters and equipment parameters for the three separation processes were obtained. Simulation results showed that water and ethylene glycol were suitable extractants for the separation system, the single solvent three column extractive distillation process was better than the double solvent four column extractive distillation process and the energy consumption could be reduced by 37.9%, TAC decreased by 38.9%. Compared with the double solvent four column extractive distillation process and single solvent three column extractive distillation process, the double solvent synergistic extractive distillation process can save energy by 45.6% and 12.4%, reduce TAC by 43.5% and 11.6%, respectively.
引文
[1]李英栋,赵雅静,李凭.差压精馏法分离甲醇与乙酸甲酯[J].能源化工,2015,36(3):19-22.Li Y D,Zhao Y J,Li P.Separation of Methanol and Methyl Acetate by Pressure Swing Distillation[J].Energy Chemical Industry,2015,36(3):19-22.
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[10]黄涛,汤志刚,段占庭.乙酸甲酯-甲醇-水体系的盐效应[J].精细化工,2003,20(6):381-384.Huang T,Tang Z G,Duan Z T.Study on the Salt Effect of Methyl Acetate-Methanol-Water System[J].Fine Chemicals,2003,20(6):381-384.
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[12]Horsely L H.Azeotropic Data III[M].Washington DC:American Chemical Society,1973,76:112-118.
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[14]Cai J L,Cui X B,Zhang Y,et al.Vapor-Liquid Equilibrium and Liquid-Liquid Equilibrium of Methyl Acetate+Methanol+1-Ethyl-3-methylimidazolium Acetate[J].Chem.Eng.Data,2010,56(2):282-287.
[15]杨德明,谭建凯,王颖,等.基于MVR热泵精馏的混合醇热集成分离工艺[J].化工进展,2015,34(11):4120-4125.Yang D M,Tan J K,Wang Y,et al.Heat Integrated Separation Technology for Separating Mixed Alcohol Based on the MVR Heatpump Distillation[J].Chemical Industry and Engineering Process,2015,34(11):4120-4125.
[2]张志刚,李倩倩,李文秀,等.萃取精馏分离乙酸甲酯-甲醇溶剂[J].化学工程,2011,39(5):36-43.Zhang Z G,Li Q Q,Li W X,et al.Mixed Solvent for Separating Methyl Acetate-Methanol by Extractive Distillation[J].Chemical Engineering,2011,39(5):36-43.
[3]田征,崔现宝,彭艳枚,等.离子液体萃取精馏分离乙酸甲酯-甲醇共沸物[J].石油化工,2013,42(5):537-541.Tian Z,Cui X B,Peng Y M,et al.Extractive Distillation of Methyl Acetate-Methanol Azeotrope with Ionic Liquid[J].Petrochemical Technology,2013,42(5):537-541.
[4]曹宇锋,顾正桂,施磊,等.液液萃取分离乙酸甲酯与甲醇水溶液的模拟计算[J].化学工程,2012,40(12):57-60.Cao Y F,Gu Z G,Shi L,et al.Modeling Calculation of Liquid-Liquid Extraction of Methyl Acetate and Methanol Aqueous Solution[J].Chemical Engineering,2012,40(12):57-60.
[5]邱挺,吴燕翔,王良恩,等.乙酸甲酯与甲醇共沸物催化精馏水解工艺[J].化工进展,2007,26(4):584-589.Qiu T,Wu Y X,Wang L E,et al.Hydrolysis of Methyl Acetate and Methanol Mixture in a Catalytic Distillation Column[J].Chemical Industry and Engineering Process,2007,26(4):584-589.
[6]张志刚,徐世民,李鑫钢,等.间歇萃取精馏技术的研究进展[J].化工进展,2004,23(9):933-937.Zhang Z G,Xu S M,Li X G,et al.Advances in Batch Extractive Distillation Technique[J].Chemical Industry and Engineering Process,2004,23(9):933-937.
[7]Seiler M,Jork C,Kavarnou A,et al.Separation of Azeotropic Mixtures Using Hyperbranched Polymers or Ionic Liquids[J].AICh E J.,2004,50(10):2439-2454.
[8]Berg L,Bozeman M T.Separation of Methanol from Methyl Acetate by Extractive Distillation:US4549938[P].1985-10-29.
[9]杨东杰,楼宏铭,庞煜霞,等.乙酸甲酯-甲醇-水的复合盐萃取分离研究[J].高校化学工程学报,2007,21(2):239-244.Yang D J,Lou H M,Pang Y X,et al.Separation of Methyl AcetateMethanol-Water by Extraction with Composite Salts[J].Journal of Chemical Engineering of Chinese Universities,2007,21(2):239-244.
[10]黄涛,汤志刚,段占庭.乙酸甲酯-甲醇-水体系的盐效应[J].精细化工,2003,20(6):381-384.Huang T,Tang Z G,Duan Z T.Study on the Salt Effect of Methyl Acetate-Methanol-Water System[J].Fine Chemicals,2003,20(6):381-384.
[11]Luyben W L.Distillation Design and Control Using ASPENTMSimulation[M].New Jersey:John Wiley&Sons,2006:112-129.
[12]Horsely L H.Azeotropic Data III[M].Washington DC:American Chemical Society,1973,76:112-118.
[13]Eckert C A,Newman B A,Nicolaides G L,et al.Measurement and Application of Limiting Activity Coefficients[J].AICHE J.,1981,27(4):33-40.
[14]Cai J L,Cui X B,Zhang Y,et al.Vapor-Liquid Equilibrium and Liquid-Liquid Equilibrium of Methyl Acetate+Methanol+1-Ethyl-3-methylimidazolium Acetate[J].Chem.Eng.Data,2010,56(2):282-287.
[15]杨德明,谭建凯,王颖,等.基于MVR热泵精馏的混合醇热集成分离工艺[J].化工进展,2015,34(11):4120-4125.Yang D M,Tan J K,Wang Y,et al.Heat Integrated Separation Technology for Separating Mixed Alcohol Based on the MVR Heatpump Distillation[J].Chemical Industry and Engineering Process,2015,34(11):4120-4125.