含HFO二元混合工质汽液相平衡性质研究
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摘要
为了提高环保替代混合制冷工质相平衡数据的计算精度,文中收集了公开发表的7种HFOs/HFCs及6种HFOs/HCs 2类二元混合工质的气液相平衡性质实验数据,分别采用PR方程+VDW混合法则、PR方程+MHV1混合法则+Wilson模型对2类混合工质的气液相平衡性质进行了非线性优化,结果表明:对于HFOs/HFCs,PR+MHV1+Wilson模型计算值与实验结果的压力平均相对偏差为0. 28%,汽相组分的平均绝对偏差为0. 003 5,PR+VDW模型的结果分别为0. 30%和0. 003 6;对于HFOs/HCs,PR+MHV1+Wilson模型计算值与实验结果的压力平均相对偏差为0. 25%,汽相组分的平均绝对偏差为0. 003 7,PR+VDW模型的结果分别为0. 55%和0. 004 8。可见:相比于PR+VDW模型,PR+MHV1+Wilson模型对HFOs/HFCs混合工质的汽液相平衡性质计算精度提升有限,对HFOs/HCs类工质则可显著提升计算精度。
In order to improve the performance of the vapor-liquid equilibria model for binary mixture containing HFO,vapor-liquid equilibrium data were collected for seven binary HFOs/HFCs and six binary HFOs/HCs system.The experimental VLE data were fitted using PR equation of state together with VDW mixing rule and PR equation of state together with MHV1 mixing rule and Wilson model for these 13 systems.For HFOs/HFCs system,the absolute average deviations in terms of saturated pressure and vapor phase composition between experimental data and PR + MHV1 + Wilson model were 0.28% and 0.003 5,respectively,the deviations between experimental data and PR + VDW model were 0.30% and 0.003 6,respectively.For HFOs/HCs system,the absolute average deviations in terms of saturated pressure and vapor phase composition between experimental data and PR + MHV1 +Wilson model were 0.25% and 0.003 7,respectively,the deviations between experimental data and PR + VDW model were 0.55% and 0.004 8,respectively.The results show that the VLE calculation accuracy is improved more significantly by PR + MHV1 + Wilson model for HFOs/HCs system than HFOs/HFCs system,compared to PR + VDW model.
In order to improve the performance of the vapor-liquid equilibria model for binary mixture containing HFO,vapor-liquid equilibrium data were collected for seven binary HFOs/HFCs and six binary HFOs/HCs system.The experimental VLE data were fitted using PR equation of state together with VDW mixing rule and PR equation of state together with MHV1 mixing rule and Wilson model for these 13 systems.For HFOs/HFCs system,the absolute average deviations in terms of saturated pressure and vapor phase composition between experimental data and PR + MHV1 + Wilson model were 0.28% and 0.003 5,respectively,the deviations between experimental data and PR + VDW model were 0.30% and 0.003 6,respectively.For HFOs/HCs system,the absolute average deviations in terms of saturated pressure and vapor phase composition between experimental data and PR + MHV1 +Wilson model were 0.25% and 0.003 7,respectively,the deviations between experimental data and PR + VDW model were 0.55% and 0.004 8,respectively.The results show that the VLE calculation accuracy is improved more significantly by PR + MHV1 + Wilson model for HFOs/HCs system than HFOs/HFCs system,compared to PR + VDW model.
引文
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[12]HU Xiaozhen,MENG Xianyang,WU Jiangtao.Isothermal vapor liquidequilibrium measurements for difluorometh-ane(R32)+trans-1,3,3,3-tetrafluoropropene(R1234ze(E))[J].Fluid Phase Equilibria,2017,431:58-65.
[13]YANG Zhi,GONG Miaoqiong,GUO Hao,et al.Phase equilibrium for the binary mixture of{1,1-difluoroethane(R152a)+trans-1,3,3,3-tetrafluoropropene(R1234ze(E))}at various temperatures from 258.150 to 288.150K[J].Fluid Phase Equilibria,2014,379:59-61.
[14]HU Peng,CHEN Longxiang,CHEN Zeshao.Vapor-liquid equilibria for binary system of 2,3,3,3-tetrafluoroprop-1-ene(HFO-1234yf)+isobutane(HC-600a)[J].Fluid Phase Equilibria,2014,365:1-4.
[15]ZHONG Quan,DONG Xueqiang,ZHAO Yanxing,et al.Measurements of isothermal vapour-liquid equilibrium for the 2,3,3,3-tetrafluoroprop-1-ene+propane system at temperatures from 253.150 to 293.150 K[J].International Journal of Refrigeration,2017,81:26-32.
[16]DONG Xueqiang,GONG Maoqiong,SHEN Jun,et al.Vapor liquid equilibria of the trans-1,3,3,3-tetrafluoropropene(R1234ze(E))+isobutane(R600a)system at various temperatures from(258.150 to 288.150)K[J].J Chem Eng Data,2012,57:541-544.
[17]DONG Xueqiang,GONG Maoqiong,SHEN Jun,et al.Experimental measurement of vapor-liquid equilibrium for(trans-1,3,3,3-tetrafluoropropene(R1234ze(E))-propane(R290))[J].International Journal of Refrigeration,2011,34:1238-1243.
[18]ZHANG Xuedong,DONG Xueqiang,GAO Hao,et al.Measurements and correlations of isothermal(vapour+liquid)equilibrium for the{isobutane(R600a)+cis-1,3,3,3-tetrafluoropropene(R1234ze(Z))}system at temperatures from(303.150 to 353.150)K[J].J Chem Thermodynamics,2016,103:349-354.
[19]GUO Maoqiong,ZHANG Yanxing,Dong Xueqiang,et al.Measurements of isothermal(vapor+liquid)equilibrium for the(propane+cis-1,3,3,3-tetrAfluoro propene)system at temperatures from(253.150 to 293.150)K[J].JChem Thermodynamics,2016,98:319-323.
[2]HODNEBROGΦ,ETMINAN M,FUGLESTVEDT J S,et al.Global warming potentials and radiative efficiencies of halocarbons and related compounds:A comprehensive review[J].Reviews of Geophysics,2013,51(2):300-378.
[3]PENG D Y,ROBINSON D B.A New two-constant equation of state[J].Ind Chem Fundam,1976,15:59-64.
[4]MICHELSEN M L.A modified Huron-vidal maxing rule for cubic equations of state[J].Fluid Phase Equilibria,1990,60(1/2):213-219.
[5]HURON M,VIDAL J.New mixing rules in simple equations of state for repressenting vapor-liquid equilibria[J].Fluid Phase Equilibria,1979,3:225-271.
[6]WILSON G M.A new expression for the excess freeenergy of mixing[J].J Am Chem Soc,1964,86:127-130.
[7]HU Peng,CHEN Longxiang,ZHU Wanbao,et al.Vaporliquid equilibria for the binary system of 2,3,3,3-tetrafluoroprop-1-ene(HFO-1234yf)+1,1,1,2,3,3,3-heptafluoropropane(HFC-227ea)[J].Fluid Phase Equilibria,2014,379:59-61.
[8]CHEN Longxiang,HU Peng,ZHU Wanbao,et al.Vaporliquid equilibria of fluoroethane(HFC-161)+2,3,3,3-tetrafluoroprop-1-ene(HFO-1234yf)[J].Fluid Phase Equilibria,2015,392:19-23.
[9]HU Peng,CHEN Longxiang,CHEN Zeshao.Vapor-liquid equilibria for the 1,1,1,2-tetrafluoroethane(HFC-134a)+1,1,1,2,3,3,3-heptafluoropropane(HFC-227ea)and 1,1,1-trifluoroethane(HFC-143a)+2,3,3,3-tetrafluoroprop-1-ene(HFO-1234yf)systems[J].Fluid Phase Equilibria,2016,414:111-116.
[10]HU Peng,CHEN Longxiang,ZHU Wanbao.Isothermal VLEmeasurements for the binary mixture of 2,3,3,3-tetrafluoroprop-1-ene(HFO-1234yf)+1,1-difluoroethane(HFC-152a)[J].Fluid Phase Equilibria,2014,373:80-83.
[11]YANG Zhiqiang,KOU Liangang,HAN Sheng,et al.Vapor-liquid equilibria of 2,3,3,3-tetrafluoropropene(HFO-1234yf)+1,1,1,2,2-pentafluoropropane(HFC-245cb)system[J].Fluid Phase Equilibria,2016,427:390-393.
[12]HU Xiaozhen,MENG Xianyang,WU Jiangtao.Isothermal vapor liquidequilibrium measurements for difluorometh-ane(R32)+trans-1,3,3,3-tetrafluoropropene(R1234ze(E))[J].Fluid Phase Equilibria,2017,431:58-65.
[13]YANG Zhi,GONG Miaoqiong,GUO Hao,et al.Phase equilibrium for the binary mixture of{1,1-difluoroethane(R152a)+trans-1,3,3,3-tetrafluoropropene(R1234ze(E))}at various temperatures from 258.150 to 288.150K[J].Fluid Phase Equilibria,2014,379:59-61.
[14]HU Peng,CHEN Longxiang,CHEN Zeshao.Vapor-liquid equilibria for binary system of 2,3,3,3-tetrafluoroprop-1-ene(HFO-1234yf)+isobutane(HC-600a)[J].Fluid Phase Equilibria,2014,365:1-4.
[15]ZHONG Quan,DONG Xueqiang,ZHAO Yanxing,et al.Measurements of isothermal vapour-liquid equilibrium for the 2,3,3,3-tetrafluoroprop-1-ene+propane system at temperatures from 253.150 to 293.150 K[J].International Journal of Refrigeration,2017,81:26-32.
[16]DONG Xueqiang,GONG Maoqiong,SHEN Jun,et al.Vapor liquid equilibria of the trans-1,3,3,3-tetrafluoropropene(R1234ze(E))+isobutane(R600a)system at various temperatures from(258.150 to 288.150)K[J].J Chem Eng Data,2012,57:541-544.
[17]DONG Xueqiang,GONG Maoqiong,SHEN Jun,et al.Experimental measurement of vapor-liquid equilibrium for(trans-1,3,3,3-tetrafluoropropene(R1234ze(E))-propane(R290))[J].International Journal of Refrigeration,2011,34:1238-1243.
[18]ZHANG Xuedong,DONG Xueqiang,GAO Hao,et al.Measurements and correlations of isothermal(vapour+liquid)equilibrium for the{isobutane(R600a)+cis-1,3,3,3-tetrafluoropropene(R1234ze(Z))}system at temperatures from(303.150 to 353.150)K[J].J Chem Thermodynamics,2016,103:349-354.
[19]GUO Maoqiong,ZHANG Yanxing,Dong Xueqiang,et al.Measurements of isothermal(vapor+liquid)equilibrium for the(propane+cis-1,3,3,3-tetrAfluoro propene)system at temperatures from(253.150 to 293.150)K[J].JChem Thermodynamics,2016,98:319-323.