循环全回流间歇精馏多温控制的研究
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摘要
循环全回流间歇精馏操作方法是近年来开发的间歇精馏新型操作方法之一。这种操作方法包括全回流浓缩和无回流采出两个基本操作状态,反复循环直到操作结束。同传统的间歇精馏过程相比,全回流操作方式能获得最高的浓缩速率,而全采出操作方式具有最大的排出速度,可在最短的时间内将轻组分从塔顶馏出,具有分离效率高、控制简便,对扰动不敏感,易于操作的优点。目前的研究基本上集中在操作方法的理论研究方面,而缺少对其优化控制的实验研究。
本文针对已有控制方法的不足,提出了循环全回流间歇精馏的一种新型控制方法—多温控制法,并建立了实验装置,以乙醇-正丙醇为实验物系,对该控制方法进行了研究。首先对循环全回流间歇精馏过程的基础—全采出过程进行了实验研究和模拟研究,然后对循环全回流间歇精馏多温控制过程的具体控制方法进行了研究,考察了不同进料浓度、温度控制点和全采出时间下多温控制过程的规律;然后在上述研究的基础上,提出了循环全回流间歇精馏多温控制法;最后在相同的实验条件下对比了单温控制法、双温控制法和本文提出的多温控制法。
实验结果表明:本文提出的多温控制法和单温控制法相比,操作时间仅增加了3%,而采出产品的体积增加了27.76%,轻组分回收率提高了19.63%;和双温控制相比,采出产品的总量和轻组分回收率降幅均不超过3.09%,而操作时间节省了35.88%;因此,和已有的单温和双温控制法相比,多温控制法可以在较短的时间内最大限度采出轻组分,同时有效防止重组分的上升,保证得到高浓度的合格产品,明显优于已有的单温控制法和双温控制法。
Cyclic total reflux operation is one of the new operating modes of batch distillation. It involves two basic operation states: total reflux and total withdrawal and the alternation of them are carried out until the whole operation is completed. This operation is one of the most promising modes of batch distillation for its unique advantages over conventional partial reflux mode in highest enriching efficiency under total reflux and fastest product collection rate under total withdrawal, together with high efficiency, energy saving and convenient controlling. Few researches are focused on the development and optimization of the control method for this new operation mode which needs more precise and optimized control in order to give full play to its potential.
To conquer the disadvantage of the former control methods, a novel control method of cyclic total reflux batch distillation without reflux drum, i.e., multi-temperature control was studied using ethanol-propanol as the experimental mixture. First, total withdrawal process was researched by experiment and simulation. Also, multi-temperature control process was explored at different feed concentrations, temperature control points and total withdrawal time. Then, multi-temperature control method was proposed accordingly. Finally, contrast experiments of single temperature control, dual-temperature control and multi-temperature control were carried out.
The results showed that compared with single temperature control, the operation time increased by only 3%, while the volume and recovery of the light component increased by 27.76% and 19.63% respectively. And compared with dual-temperature control, the volume and recovery of the light component decreased by no more than 3.09%, while the operation time saved by 35.88%. So it can be seen that compared with single temperature control and dual-temperature control, more light component was collected in shorter time by multi-temperature control. At the same time, the heavy component was effectively kept in the lower part of the column and high concentration of the distillate is assured. Therefore, the novel multi-temperature control method holds obvious advantage over the other two control methods.
本文针对已有控制方法的不足,提出了循环全回流间歇精馏的一种新型控制方法—多温控制法,并建立了实验装置,以乙醇-正丙醇为实验物系,对该控制方法进行了研究。首先对循环全回流间歇精馏过程的基础—全采出过程进行了实验研究和模拟研究,然后对循环全回流间歇精馏多温控制过程的具体控制方法进行了研究,考察了不同进料浓度、温度控制点和全采出时间下多温控制过程的规律;然后在上述研究的基础上,提出了循环全回流间歇精馏多温控制法;最后在相同的实验条件下对比了单温控制法、双温控制法和本文提出的多温控制法。
实验结果表明:本文提出的多温控制法和单温控制法相比,操作时间仅增加了3%,而采出产品的体积增加了27.76%,轻组分回收率提高了19.63%;和双温控制相比,采出产品的总量和轻组分回收率降幅均不超过3.09%,而操作时间节省了35.88%;因此,和已有的单温和双温控制法相比,多温控制法可以在较短的时间内最大限度采出轻组分,同时有效防止重组分的上升,保证得到高浓度的合格产品,明显优于已有的单温控制法和双温控制法。
Cyclic total reflux operation is one of the new operating modes of batch distillation. It involves two basic operation states: total reflux and total withdrawal and the alternation of them are carried out until the whole operation is completed. This operation is one of the most promising modes of batch distillation for its unique advantages over conventional partial reflux mode in highest enriching efficiency under total reflux and fastest product collection rate under total withdrawal, together with high efficiency, energy saving and convenient controlling. Few researches are focused on the development and optimization of the control method for this new operation mode which needs more precise and optimized control in order to give full play to its potential.
To conquer the disadvantage of the former control methods, a novel control method of cyclic total reflux batch distillation without reflux drum, i.e., multi-temperature control was studied using ethanol-propanol as the experimental mixture. First, total withdrawal process was researched by experiment and simulation. Also, multi-temperature control process was explored at different feed concentrations, temperature control points and total withdrawal time. Then, multi-temperature control method was proposed accordingly. Finally, contrast experiments of single temperature control, dual-temperature control and multi-temperature control were carried out.
The results showed that compared with single temperature control, the operation time increased by only 3%, while the volume and recovery of the light component increased by 27.76% and 19.63% respectively. And compared with dual-temperature control, the volume and recovery of the light component decreased by no more than 3.09%, while the operation time saved by 35.88%. So it can be seen that compared with single temperature control and dual-temperature control, more light component was collected in shorter time by multi-temperature control. At the same time, the heavy component was effectively kept in the lower part of the column and high concentration of the distillate is assured. Therefore, the novel multi-temperature control method holds obvious advantage over the other two control methods.
引文
[1]时钧,余国琮等,物理学,化学工程手册,第二版,北京:化学工业出版社,1996.13
[2]白鹏,姜健,张志等,间歇精馏新型操作方式的研究进展,化学工业与工程,17(4):226~229,245
[3]杨海荣,薄翠梅,陆爱晶等,间歇精馏变回流比智能控制法的研究,化工自动化与仪表,2008,35(1):12~16
[4]李贞玉,李长海,汤洁等,基于间歇精馏回收废溶剂中二甲苯/醋酸丁酯,环境工程学报,2008,4:564~568
[5]颜清,彭小平,冷明伟,VBA实现恒馏出液组成间歇精馏的计算机模拟,计算机应用与软件,2008,25(12):88~90,102
[6]许松林,应安国,王淑华,桃醛提纯的真空间歇精馏工艺,化学工业与工程,2005,22(2):112~114,144
[7]陈建宁,阮奇,陈佳彬等,间歇精馏常规设计和优化设计的模型和算法,计算机与应用化学,2004,21(3):429~433
[8]白鹏,张健,姜志等,间歇精馏新型操作方式的研究进展,化学工业与工程,2000,17(4):226~230
[9]Arthur Rose R L,Williams T J,and Charles Prevost.Holdup in Batch Distillation.Industrial and Engineering Chemistry,1950,42(9):1876~1879
[10]Pigford J B.Effect of Column Holdup in Batch Distillation.Industrial and Engineering Chemistry,1951,43(11):2592~2602
[11]Trilleros Villaverde J A,Otero de la Gandara J L.Analogical Study of the Unsteady State in A Rectifying Column Operating under Total Reflux(I)Theretical Aspects.International Chemical Engineering AIChE,1994,34(3):320~327
[12]Mori Hideki,Ito Chikara,and Oda Akiyoshi,et al.Total Reflux Simulation of Packed Column Distillation.Journal of Chemical Engineering of Japan,1999,32(1):69~75
[13]白鹏,张卫江,余国琮,动态累积分批精馏过程研究(1),化学工程,1994,22(5):15
[14]Davidyan A G,Kiva V N,and Platonov V M.Separation of binary mixtures in two-section column with central reservoir.Theory Found Chemical Engineering, 1992,25(4):393~400
[15]白鹏,张卫江,尹波等,无返混动态累积分批精馏过程,化学工程,2000,28(5):7~9
[16]李文秀,胡国良,于三三,间歇精馏过度馏分的脉动馏出,沈阳化工学院学报,1996,10(3):196~201
[17]郭天仁,白鹏,曹吉林,间歇精馏过渡馏份的脉冲控制法,化工科技,1999,7 (4) :15～18
[18]曲红梅,张卫江,白鹏等,分批精馏最小过渡馏分量及过渡馏分脉冲控制法的研究,2002,30(6):7~11
[19]朱良伟,间歇精馏全回流浓缩-无回流采出过程的研究:[硕士学位论文],天津:天津大学,2006
[20]刘佳,循环全回流间歇精馏操作和模拟计算研究:[硕士学位论文],天津:天津大学,2006
[21]González-Velasco J R,AGutiérrez-Ortiz M,and Castresana-Pelayo J M,et al.Improvements in Batch Distillation Startup.Ind.Eng.Chem.Res.,1987,26(4):745
[22]Pigford R L.Effect of Column Holdup in Batch Distillation.Ind.Eng.Chem., 1951,43(11):2592
[23]李文秀,间歇精馏塔理论板数的一种确定方法,化工设计,1995,5(4):28~31
[24]Converse A O,and Gross G D.Optimal Distillate Rate Policy in Batch Distillation.Ind.Eng Chem.Fundum,1963,2:217
[25]王为国,冯魏良,彭友瑞等,二元多段恒回流比常规间歇精馏的讨论,设计技术,2008,18(1):7~9
[26]杨海荣,薄翠梅,陆爱晶等,间歇精馏过程变回流比智能控制法的研究,化工自动化及仪表,2008,35(1):12~16
[27]颜青,彭小平,恒馏出液组成间歇精馏回流比的控制和调节,2008,25(10):1248~1252
[28]张雪梅,张卫江,简春贵等,多组元分批精馏中各种设计参数对回流比的影响,化工进展,2004,23(5):519~523
[29]王心满,苑静,佟瑞栋,间歇精馏最小回流比的近似计算及其应用,辽宁师专学报,1999:38~39
[30]曾真,毕亚凡,二元混合物恒回流比间歇精馏的捷算法,武汉化工学院学报,2000,22(1):16~19
[31]Enrique Q M,William L Luyben.Inferential Model-based Control of Multi-component Batch distillation.Chem.Eng.Sci.,1992,47(4):887~898
[32]刘芳,高炉铁水温度的神经网络软测量及应用冶金自动化,2006(S2):148~151
[33]Süleyman Karacan.Application of a non-linear long range predictive control to a packed distillation column. Chemical Engineering and Processing,2003,42: 943~953
[34]Zumoffen L.Garyulo,M.Basualdo,L.Jiménez.Computer Aided Chemical Engineering,2005,20(2):1465~1470
[35]曾舟华,不稳定精馏恒馏出液组成回流比的自动控制,黄冈师专学报,1997,1:70~72
[36] William L.Luyben.Evaluation of criteria for selecting temperature control trays in distillation columns.Journal of Process Control,2006,16(2):115~134
[37]刘成军,刘登峰,薛发芳,精馏控制系统中灵敏板的求取,石油与天然气化工,1997,26(3):179~181
[38]Converse A O,Gross G D.Optimal Distillate Rate Policy in Batch Distillation.Ind.Eng Chem.Fundum,1963,2:217
[39]Kerkhof L H J , Vissers H J M . On the Profit of Optimum Control in Batch Distillation.Chem.Eng.Sci.,1978,33(3/4):961~970
[40]Robinson E R.The Optimization of Batch Distillation Operation.Chem.Eng.Sci.,1969,24:1661~1668
[41]宋海华,精馏模拟,天津:天津大学出版社,2005:287~288
[42]Arthur Rose , Curtis Johnson R and Williams T J . Batch Fractional Distillation.Ind. Eng.Chem.,1950,42(10):2145~2149
[43]Charles E , Huckaba and Donald E . Calculation Procedures for Binary Batch Rectification.AIChE Journal,1960,6(2):335~342
[44]Distefano G P.Mathematical Modeling and Numberical Integration of Multicomponent Batch Distillation Equation.AIChE Journal,1968,14(1):190~199
[45]Distefano G.P.Stability of Numerical Integration Techniques.AIChE Journal,1968,14(6):946~955
[46]Joseph F.Boston,Herbert I.and Britt,et al.An Advanced System for the Simulation of Batch Distillation Operation.Foundations of Computer-Aided Chemical Process Design,1982,2:203~237
[47]Steven E.Gallun,Charles D.Holland.Gear’s Procedure for the Simultaneous Solution of Differential and Application to Unsteady State Distillation Problems.Computers and Chemical Engineering,1982,6(3):231~244
[48]H . Sadotomo , Miyahara K . Calculation Procedure for Multicomponent Batch Distillation.International Chemical Engineering,1983,23(1):56~64
[49]Galindez H , Fredenslund A . Simulation of Multicomponent Batch Distillation Processes.Computers and Chemical Engineering,1988,12(4):281~288
[50]吴迪,分批精馏过程的模拟和设计计算方法的研究:[硕士生学位论文],天津:天津大学,1992
[51] Urmila M Diwekar,Madhavan K P.Multicomponent Batch Distillation Column Design.Ind.Eng.Chem.Res.,1991,30:713~721
[52] Suresh Sundaram,Lawrence B.Evans.Shortcut Procedure for Simulating Batch Distillation Operations.Ind.Eng.Chem.Res.,1993,32:511~518
[53]Urmila M Diwekar . How Simple Can it be?-A Look at the Models for Batch Distillation.Computers Chem.Eng.,1994,18:suppl.:451~457
[54]Bauerle G L,Sandall O C.Batch Distillation of Binary Mixtures at Minimum Reflux.AIChE Journal,1978,33(6):1034
[55]金克新,赵传钧,马沛生,化工热力学,天津:天津大学出版社,1997.141~144
[2]白鹏,姜健,张志等,间歇精馏新型操作方式的研究进展,化学工业与工程,17(4):226~229,245
[3]杨海荣,薄翠梅,陆爱晶等,间歇精馏变回流比智能控制法的研究,化工自动化与仪表,2008,35(1):12~16
[4]李贞玉,李长海,汤洁等,基于间歇精馏回收废溶剂中二甲苯/醋酸丁酯,环境工程学报,2008,4:564~568
[5]颜清,彭小平,冷明伟,VBA实现恒馏出液组成间歇精馏的计算机模拟,计算机应用与软件,2008,25(12):88~90,102
[6]许松林,应安国,王淑华,桃醛提纯的真空间歇精馏工艺,化学工业与工程,2005,22(2):112~114,144
[7]陈建宁,阮奇,陈佳彬等,间歇精馏常规设计和优化设计的模型和算法,计算机与应用化学,2004,21(3):429~433
[8]白鹏,张健,姜志等,间歇精馏新型操作方式的研究进展,化学工业与工程,2000,17(4):226~230
[9]Arthur Rose R L,Williams T J,and Charles Prevost.Holdup in Batch Distillation.Industrial and Engineering Chemistry,1950,42(9):1876~1879
[10]Pigford J B.Effect of Column Holdup in Batch Distillation.Industrial and Engineering Chemistry,1951,43(11):2592~2602
[11]Trilleros Villaverde J A,Otero de la Gandara J L.Analogical Study of the Unsteady State in A Rectifying Column Operating under Total Reflux(I)Theretical Aspects.International Chemical Engineering AIChE,1994,34(3):320~327
[12]Mori Hideki,Ito Chikara,and Oda Akiyoshi,et al.Total Reflux Simulation of Packed Column Distillation.Journal of Chemical Engineering of Japan,1999,32(1):69~75
[13]白鹏,张卫江,余国琮,动态累积分批精馏过程研究(1),化学工程,1994,22(5):15
[14]Davidyan A G,Kiva V N,and Platonov V M.Separation of binary mixtures in two-section column with central reservoir.Theory Found Chemical Engineering, 1992,25(4):393~400
[15]白鹏,张卫江,尹波等,无返混动态累积分批精馏过程,化学工程,2000,28(5):7~9
[16]李文秀,胡国良,于三三,间歇精馏过度馏分的脉动馏出,沈阳化工学院学报,1996,10(3):196~201
[17]郭天仁,白鹏,曹吉林,间歇精馏过渡馏份的脉冲控制法,化工科技,1999,7 (4) :15～18
[18]曲红梅,张卫江,白鹏等,分批精馏最小过渡馏分量及过渡馏分脉冲控制法的研究,2002,30(6):7~11
[19]朱良伟,间歇精馏全回流浓缩-无回流采出过程的研究:[硕士学位论文],天津:天津大学,2006
[20]刘佳,循环全回流间歇精馏操作和模拟计算研究:[硕士学位论文],天津:天津大学,2006
[21]González-Velasco J R,AGutiérrez-Ortiz M,and Castresana-Pelayo J M,et al.Improvements in Batch Distillation Startup.Ind.Eng.Chem.Res.,1987,26(4):745
[22]Pigford R L.Effect of Column Holdup in Batch Distillation.Ind.Eng.Chem., 1951,43(11):2592
[23]李文秀,间歇精馏塔理论板数的一种确定方法,化工设计,1995,5(4):28~31
[24]Converse A O,and Gross G D.Optimal Distillate Rate Policy in Batch Distillation.Ind.Eng Chem.Fundum,1963,2:217
[25]王为国,冯魏良,彭友瑞等,二元多段恒回流比常规间歇精馏的讨论,设计技术,2008,18(1):7~9
[26]杨海荣,薄翠梅,陆爱晶等,间歇精馏过程变回流比智能控制法的研究,化工自动化及仪表,2008,35(1):12~16
[27]颜青,彭小平,恒馏出液组成间歇精馏回流比的控制和调节,2008,25(10):1248~1252
[28]张雪梅,张卫江,简春贵等,多组元分批精馏中各种设计参数对回流比的影响,化工进展,2004,23(5):519~523
[29]王心满,苑静,佟瑞栋,间歇精馏最小回流比的近似计算及其应用,辽宁师专学报,1999:38~39
[30]曾真,毕亚凡,二元混合物恒回流比间歇精馏的捷算法,武汉化工学院学报,2000,22(1):16~19
[31]Enrique Q M,William L Luyben.Inferential Model-based Control of Multi-component Batch distillation.Chem.Eng.Sci.,1992,47(4):887~898
[32]刘芳,高炉铁水温度的神经网络软测量及应用冶金自动化,2006(S2):148~151
[33]Süleyman Karacan.Application of a non-linear long range predictive control to a packed distillation column. Chemical Engineering and Processing,2003,42: 943~953
[34]Zumoffen L.Garyulo,M.Basualdo,L.Jiménez.Computer Aided Chemical Engineering,2005,20(2):1465~1470
[35]曾舟华,不稳定精馏恒馏出液组成回流比的自动控制,黄冈师专学报,1997,1:70~72
[36] William L.Luyben.Evaluation of criteria for selecting temperature control trays in distillation columns.Journal of Process Control,2006,16(2):115~134
[37]刘成军,刘登峰,薛发芳,精馏控制系统中灵敏板的求取,石油与天然气化工,1997,26(3):179~181
[38]Converse A O,Gross G D.Optimal Distillate Rate Policy in Batch Distillation.Ind.Eng Chem.Fundum,1963,2:217
[39]Kerkhof L H J , Vissers H J M . On the Profit of Optimum Control in Batch Distillation.Chem.Eng.Sci.,1978,33(3/4):961~970
[40]Robinson E R.The Optimization of Batch Distillation Operation.Chem.Eng.Sci.,1969,24:1661~1668
[41]宋海华,精馏模拟,天津:天津大学出版社,2005:287~288
[42]Arthur Rose , Curtis Johnson R and Williams T J . Batch Fractional Distillation.Ind. Eng.Chem.,1950,42(10):2145~2149
[43]Charles E , Huckaba and Donald E . Calculation Procedures for Binary Batch Rectification.AIChE Journal,1960,6(2):335~342
[44]Distefano G P.Mathematical Modeling and Numberical Integration of Multicomponent Batch Distillation Equation.AIChE Journal,1968,14(1):190~199
[45]Distefano G.P.Stability of Numerical Integration Techniques.AIChE Journal,1968,14(6):946~955
[46]Joseph F.Boston,Herbert I.and Britt,et al.An Advanced System for the Simulation of Batch Distillation Operation.Foundations of Computer-Aided Chemical Process Design,1982,2:203~237
[47]Steven E.Gallun,Charles D.Holland.Gear’s Procedure for the Simultaneous Solution of Differential and Application to Unsteady State Distillation Problems.Computers and Chemical Engineering,1982,6(3):231~244
[48]H . Sadotomo , Miyahara K . Calculation Procedure for Multicomponent Batch Distillation.International Chemical Engineering,1983,23(1):56~64
[49]Galindez H , Fredenslund A . Simulation of Multicomponent Batch Distillation Processes.Computers and Chemical Engineering,1988,12(4):281~288
[50]吴迪,分批精馏过程的模拟和设计计算方法的研究:[硕士生学位论文],天津:天津大学,1992
[51] Urmila M Diwekar,Madhavan K P.Multicomponent Batch Distillation Column Design.Ind.Eng.Chem.Res.,1991,30:713~721
[52] Suresh Sundaram,Lawrence B.Evans.Shortcut Procedure for Simulating Batch Distillation Operations.Ind.Eng.Chem.Res.,1993,32:511~518
[53]Urmila M Diwekar . How Simple Can it be?-A Look at the Models for Batch Distillation.Computers Chem.Eng.,1994,18:suppl.:451~457
[54]Bauerle G L,Sandall O C.Batch Distillation of Binary Mixtures at Minimum Reflux.AIChE Journal,1978,33(6):1034
[55]金克新,赵传钧,马沛生,化工热力学,天津:天津大学出版社,1997.141~144