分隔塔型热耦合精馏技术研究
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摘要
精馏是化工领域中应用广泛的单元操作,同时也是工业中能耗和设备投资高的单元操作,在石油、化工和天然气加工工业中,其能耗占全过程总能耗的一半以上。因此对精馏过程节能技术的研究具有极其重要的意义。
热耦精馏是用主塔和副塔组成的复杂塔序,它可以降低过程中的不可逆有效能损失,提高热力学效率。分隔壁精馏塔是热耦精馏的特殊塔结构,具有节能、投资低的优点。
本文以分离三组分混合物为研究对象,采用化工模拟软件Aspen Plus对三种分隔壁精馏塔和常规精馏序列进行模拟分析,考察了不同进料组成及分离指数(ESI)对各塔序能耗的影响。
本文还以工业催化重整脱戊烷油中苯、甲苯、二甲苯混合物的分离进行实际应用模拟,发现进料位置、回流比、侧线采出位置、液体分配比均对分离效果产生影响。并对比分隔壁精馏流程、常规侧线采出和常规精馏流程,结果表明,分隔壁精馏塔分离效果、能耗均具有一定优势,并分析了节能原因。
Distillation,which has high energy consumption and needs costly equipment,is.widely used unit operation in chemical industry.In the industry of crude oil refine,chemical engineering and natural gas processing,its energy consumption is more than half of total process energy consumption.So the research about saving energy on distillation process is significant.
Thermally coupled distillation is a kind of complex column process which consists of main column and accessory column.It has much less irreversible energy loss and higher Thermodynamic Efficiency in distillation process.Divided Wall Column is kind of special column structure of Thermally coupled distillation,which has less energy consumption and less cost in equipment.
The research is about separating ternary mixtures,stimulating and analyzing process of three kings of Divided Wall Column and normal Distillation with Aspen Plus software,and researching on how different feed compositions and Ease of Separation Index(ESI) influence energy consumption of every column sequences.
Simulating the mixture of benzene and toluene and dimethyl benzene from Catalytic Reforming and taking off pentane,the result showed that the feed position,reflux ratio,side -draw position and flow distribution ratio had influence in separation result.Comparing the Divided Wall Column distillation,the traditional side-draw and the traditional distillation sequence,it showed that the Divided Wall Column distillation was excellent in the separation efficiency and the energy consumption,and analyzed why it consumed less energy.
热耦精馏是用主塔和副塔组成的复杂塔序,它可以降低过程中的不可逆有效能损失,提高热力学效率。分隔壁精馏塔是热耦精馏的特殊塔结构,具有节能、投资低的优点。
本文以分离三组分混合物为研究对象,采用化工模拟软件Aspen Plus对三种分隔壁精馏塔和常规精馏序列进行模拟分析,考察了不同进料组成及分离指数(ESI)对各塔序能耗的影响。
本文还以工业催化重整脱戊烷油中苯、甲苯、二甲苯混合物的分离进行实际应用模拟,发现进料位置、回流比、侧线采出位置、液体分配比均对分离效果产生影响。并对比分隔壁精馏流程、常规侧线采出和常规精馏流程,结果表明,分隔壁精馏塔分离效果、能耗均具有一定优势,并分析了节能原因。
Distillation,which has high energy consumption and needs costly equipment,is.widely used unit operation in chemical industry.In the industry of crude oil refine,chemical engineering and natural gas processing,its energy consumption is more than half of total process energy consumption.So the research about saving energy on distillation process is significant.
Thermally coupled distillation is a kind of complex column process which consists of main column and accessory column.It has much less irreversible energy loss and higher Thermodynamic Efficiency in distillation process.Divided Wall Column is kind of special column structure of Thermally coupled distillation,which has less energy consumption and less cost in equipment.
The research is about separating ternary mixtures,stimulating and analyzing process of three kings of Divided Wall Column and normal Distillation with Aspen Plus software,and researching on how different feed compositions and Ease of Separation Index(ESI) influence energy consumption of every column sequences.
Simulating the mixture of benzene and toluene and dimethyl benzene from Catalytic Reforming and taking off pentane,the result showed that the feed position,reflux ratio,side -draw position and flow distribution ratio had influence in separation result.Comparing the Divided Wall Column distillation,the traditional side-draw and the traditional distillation sequence,it showed that the Divided Wall Column distillation was excellent in the separation efficiency and the energy consumption,and analyzed why it consumed less energy.
引文
[1]荣本光,韩方煜.具有热集成精馏流程的综合[J].青岛化工学院学报,1997.
[2]吕向红,陆恩锡.热耦蒸馏及其选用原则[J].化学工程,2005.4.
[3]陈桂珍.隔板蒸馏塔技术及其在空气分离中的潜在应用[J].设计制造,100929425(2005)062001 1204.
[4]吴俊生,邵惠鹤.精馏设计,操作和控制[M].北京:中国石化出版社,1997.
[5]Agrawal R.More operable fully thermally coupled distillation column configurations for multicomponent[J].Int J Multiphase flow,1997,23:25-36.
[6]Amm inudin K A,Smith R.Design and optimization of fully thermally coupled distillation columns,Part 2:App lication of dividing wall columns in retrofit[J].Trans,IChemE,2002,79(10):716-724.
[7]Van Zile,Charles P,Harris.Dividing wall column control system:US,6551465[P].2003-04-33.
[8]Mueller I,Kloeker M,Kenig E Y.Rate2based modeling of dividing wall columns:A new application to reactive systems[J].Proc PRES 2004.
[9]韩方煜,郑世清,荣本光.过程系统稳态模拟技术[M].北京:中国石化出版社,1999.
[10]杨友麒.实用化工系统工程[M].北京:化学工业出版社,1989
[11]张瑞生等.过程系统工程概论[M].北京:科学出版社,2001
[12]杨冀宏等.过程系统工程导论[M].北京:烃加工出版社,1989
[13]Richard Darton,"Distillation and absorption97"[J].Institution of Chemical Engineers,1997.
[14]蒋维钧,蓄良恒,刘茅林等.化工原理[M].北京:清华大学出版社,2003.
[15]宋华,陈颖.化工分离工程[M].哈尔滨:哈尔滨工业大学出版社,2003.
[16]郭天民.多元气一液平衡和精馏[M].北京:石油工业出版社,2002.
[17]Angeli P,Hewitt G F.Pressure gradient in horizontal 1iquid21iquid flows[J].Int J Multiphase Flow,1998,24:1183-1203.
[18]牛冬梅,苏新军,王树众,等.水平管内油气水三相流动摩擦压降特性的实验研究[J].油气储运,2002,21:28-31.
[19]Brinkman H C.The viscosity of concentrated suspensions and solutions[J].J Chem Physics,1952,20:571-581.
[20]NadlerM,Mewes D.Flow induced emulsification in the flow of two immiscible liquids in horizontal p ipes[J].Int J Multiphase flow,1997,23:55-8.
[21]Ammundin K A,Smith R,Thong D Y2C,etal.Design and optimization of fully thermally coupled distillation columns[J].A ICHE J,2001,79(10):701-724.
[22]Kim Y H.Rigorous design of fully thermally coupled distillation column[J].J of Chem Eng of Japan,2001,34(2):236—243.
[23]Rev E,Emitir M,Szitkai Z,et al.Energy-savings of integrated and coupled distillation systems[J].Computers & Chem Eng,2001,25(1):119—140.
[24]Mueller I.Kloeker M,Kenig E Y.Rate2based modeling of dividing wall columns:A new application to reactive systems[J].Proc PRES 2004.
[25]Petlyuk F.B.,Platonov V.M.& Avetvan V.S.,Khim.Prom[J].1966,42,No.11.865
[26]Fidkowski Z.T.& Krolikowski L,Thermally Coupled System of Distillation Columns:Optimization Procedure.AIChE J[J].1986,32(4),537.546.
[27]Fidkowski Z.T.& Krolikowski L.,Minimum Energy Requirements of Thermally Coupled Distillation Systems.AIChE J[J].1987,33(4),643.653.
[28]钱宏义．分隔塔装置的最小能耗分析及优化设计[D]．硕士论文,2004．
[29]Petlyuk F.B.Platonov V.M.ASlavinskii D.M.Thermodynamically Optimal Method for Separating Multi Component Mixtures,Int.Chem.Eng[J].1965,5(3),555-561.
[30]Triantafyllou C.& Smith R.,The Design and Optimization of Fully Thermally Coupled Distillation Columns,Trans.Inst.Chem[J].1992,70,118.132.
[31]Stupin W.J.PhD Thesis[J].University of Southern California,USA,1970.
[32]Cerda J.& Westerberg W[J].72nd AIChE Annual Meeting,San Francisco,1979.
[33]Fidkowski Z.T.& Krolikowski L.Thermally Coupled System of Distillation Columns:Optimization Procedure.AIChE J[J].1986,32(4),537.546.
[34]Carlberg N.A.& Westerberg,A.W.Temperature heat diagrams for complex columns.Underwood's method for side strippers and enrichers,Ind.Eng.Chem.Res[J],1989,28,1379.1386.
[35]Abdul Mutalib M I,Smith R.Operation and control of dividing wall columns[J].Trans Inst Chem Eng,Part A,Part A,Chem Eng Res Des,1998,76:3082334.
[36]Agrawal R.Multicomponent distillation columns with partition and multiple reboi(?)ers and condensers[J].Ind Eng Chem Res,2001,40:425824266.
[37]Guido D,Constantinos C.Optimal design of thermally coupled distillation columns[J].Ind Eng Chem Res,1999,38:1622176.
[38]Lestak F,C Collins.Advanced distillation saves energy and capital[J].Chem Eng,1997,104(7):72276.
[39]Michael A Schultz,Douglas G Stewart.Reduce costs with dividing-wall columns[J].CEP,2002,(5):64271.
[40]Triantafyllou C,Smith R.The design and optimization of fully thermally coupled distillation columns[J].Trans Inst Chem Eng,Part A:Chem Eng Res Des,1992,70:1182132.
[41]Muralikrishna K,Madhavan K P.Development of dividing wall distillation column design space for a specified separation[J].Trans Inst Chem Eng,Part A:Chem Eng Res Des,2002,80:1552176.
[42]Wolff E,Slogestad S.Operation of Petlyuk distillation columns[J].Ind Eng Chem Res,1995,34:209722112.
[43]Kellogg M W.Limited press release[R].1998209211.
[44]N ichael A Schultz,Douglas G Stewart,James M Harris.Reduce costs with dividingwall columns[J].A IChE Journal,2002(5):64.
[45]Hairston D.The divide in distillation[J].Chem Eng,1999,32.
[46]SchutzM,StewartD.Reduce the costswith dividing2wallcolumns[J].Chem Eng Prog,2002,98(5):64-71.
[47]刘兆凯 段文立.隔板精馏技术的研究进展和应用现状[M].石油化工与节能,2007.2.
[48]裘兆蓉.国内外分隔壁精馏塔现状与发展趋势[J].江苏工业学院学报,2005,17:58-61.
[49]TedderDW,Rudd D F.Parametric studies in industrial distillation:Part 1.Design comparisons[J].A ICHE J,1978,24(1):303.
[50]孙巍,李琳,陈晓春,戴燕红.基于混合模型法的精馏塔热耦合技术研究[M].现代化工,2005.7
[51]冯霄,李勤凌.化工原理节能与技术[M].北京:化学工业出版社,1998.
[2]吕向红,陆恩锡.热耦蒸馏及其选用原则[J].化学工程,2005.4.
[3]陈桂珍.隔板蒸馏塔技术及其在空气分离中的潜在应用[J].设计制造,100929425(2005)062001 1204.
[4]吴俊生,邵惠鹤.精馏设计,操作和控制[M].北京:中国石化出版社,1997.
[5]Agrawal R.More operable fully thermally coupled distillation column configurations for multicomponent[J].Int J Multiphase flow,1997,23:25-36.
[6]Amm inudin K A,Smith R.Design and optimization of fully thermally coupled distillation columns,Part 2:App lication of dividing wall columns in retrofit[J].Trans,IChemE,2002,79(10):716-724.
[7]Van Zile,Charles P,Harris.Dividing wall column control system:US,6551465[P].2003-04-33.
[8]Mueller I,Kloeker M,Kenig E Y.Rate2based modeling of dividing wall columns:A new application to reactive systems[J].Proc PRES 2004.
[9]韩方煜,郑世清,荣本光.过程系统稳态模拟技术[M].北京:中国石化出版社,1999.
[10]杨友麒.实用化工系统工程[M].北京:化学工业出版社,1989
[11]张瑞生等.过程系统工程概论[M].北京:科学出版社,2001
[12]杨冀宏等.过程系统工程导论[M].北京:烃加工出版社,1989
[13]Richard Darton,"Distillation and absorption97"[J].Institution of Chemical Engineers,1997.
[14]蒋维钧,蓄良恒,刘茅林等.化工原理[M].北京:清华大学出版社,2003.
[15]宋华,陈颖.化工分离工程[M].哈尔滨:哈尔滨工业大学出版社,2003.
[16]郭天民.多元气一液平衡和精馏[M].北京:石油工业出版社,2002.
[17]Angeli P,Hewitt G F.Pressure gradient in horizontal 1iquid21iquid flows[J].Int J Multiphase Flow,1998,24:1183-1203.
[18]牛冬梅,苏新军,王树众,等.水平管内油气水三相流动摩擦压降特性的实验研究[J].油气储运,2002,21:28-31.
[19]Brinkman H C.The viscosity of concentrated suspensions and solutions[J].J Chem Physics,1952,20:571-581.
[20]NadlerM,Mewes D.Flow induced emulsification in the flow of two immiscible liquids in horizontal p ipes[J].Int J Multiphase flow,1997,23:55-8.
[21]Ammundin K A,Smith R,Thong D Y2C,etal.Design and optimization of fully thermally coupled distillation columns[J].A ICHE J,2001,79(10):701-724.
[22]Kim Y H.Rigorous design of fully thermally coupled distillation column[J].J of Chem Eng of Japan,2001,34(2):236—243.
[23]Rev E,Emitir M,Szitkai Z,et al.Energy-savings of integrated and coupled distillation systems[J].Computers & Chem Eng,2001,25(1):119—140.
[24]Mueller I.Kloeker M,Kenig E Y.Rate2based modeling of dividing wall columns:A new application to reactive systems[J].Proc PRES 2004.
[25]Petlyuk F.B.,Platonov V.M.& Avetvan V.S.,Khim.Prom[J].1966,42,No.11.865
[26]Fidkowski Z.T.& Krolikowski L,Thermally Coupled System of Distillation Columns:Optimization Procedure.AIChE J[J].1986,32(4),537.546.
[27]Fidkowski Z.T.& Krolikowski L.,Minimum Energy Requirements of Thermally Coupled Distillation Systems.AIChE J[J].1987,33(4),643.653.
[28]钱宏义．分隔塔装置的最小能耗分析及优化设计[D]．硕士论文,2004．
[29]Petlyuk F.B.Platonov V.M.ASlavinskii D.M.Thermodynamically Optimal Method for Separating Multi Component Mixtures,Int.Chem.Eng[J].1965,5(3),555-561.
[30]Triantafyllou C.& Smith R.,The Design and Optimization of Fully Thermally Coupled Distillation Columns,Trans.Inst.Chem[J].1992,70,118.132.
[31]Stupin W.J.PhD Thesis[J].University of Southern California,USA,1970.
[32]Cerda J.& Westerberg W[J].72nd AIChE Annual Meeting,San Francisco,1979.
[33]Fidkowski Z.T.& Krolikowski L.Thermally Coupled System of Distillation Columns:Optimization Procedure.AIChE J[J].1986,32(4),537.546.
[34]Carlberg N.A.& Westerberg,A.W.Temperature heat diagrams for complex columns.Underwood's method for side strippers and enrichers,Ind.Eng.Chem.Res[J],1989,28,1379.1386.
[35]Abdul Mutalib M I,Smith R.Operation and control of dividing wall columns[J].Trans Inst Chem Eng,Part A,Part A,Chem Eng Res Des,1998,76:3082334.
[36]Agrawal R.Multicomponent distillation columns with partition and multiple reboi(?)ers and condensers[J].Ind Eng Chem Res,2001,40:425824266.
[37]Guido D,Constantinos C.Optimal design of thermally coupled distillation columns[J].Ind Eng Chem Res,1999,38:1622176.
[38]Lestak F,C Collins.Advanced distillation saves energy and capital[J].Chem Eng,1997,104(7):72276.
[39]Michael A Schultz,Douglas G Stewart.Reduce costs with dividing-wall columns[J].CEP,2002,(5):64271.
[40]Triantafyllou C,Smith R.The design and optimization of fully thermally coupled distillation columns[J].Trans Inst Chem Eng,Part A:Chem Eng Res Des,1992,70:1182132.
[41]Muralikrishna K,Madhavan K P.Development of dividing wall distillation column design space for a specified separation[J].Trans Inst Chem Eng,Part A:Chem Eng Res Des,2002,80:1552176.
[42]Wolff E,Slogestad S.Operation of Petlyuk distillation columns[J].Ind Eng Chem Res,1995,34:209722112.
[43]Kellogg M W.Limited press release[R].1998209211.
[44]N ichael A Schultz,Douglas G Stewart,James M Harris.Reduce costs with dividingwall columns[J].A IChE Journal,2002(5):64.
[45]Hairston D.The divide in distillation[J].Chem Eng,1999,32.
[46]SchutzM,StewartD.Reduce the costswith dividing2wallcolumns[J].Chem Eng Prog,2002,98(5):64-71.
[47]刘兆凯 段文立.隔板精馏技术的研究进展和应用现状[M].石油化工与节能,2007.2.
[48]裘兆蓉.国内外分隔壁精馏塔现状与发展趋势[J].江苏工业学院学报,2005,17:58-61.
[49]TedderDW,Rudd D F.Parametric studies in industrial distillation:Part 1.Design comparisons[J].A ICHE J,1978,24(1):303.
[50]孙巍,李琳,陈晓春,戴燕红.基于混合模型法的精馏塔热耦合技术研究[M].现代化工,2005.7
[51]冯霄,李勤凌.化工原理节能与技术[M].北京:化学工业出版社,1998.