含氮气的二元系统相平衡及其计算
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摘要
随着相平衡研究的发展,更多体系的相平衡数据通过不同方法得到测量和计算。作为空气中含量最多的气体N_2,有关其相平衡特别是与酯类系统的研究甚少。为了弥补这一空白,本文选择了N_2作为研究对象,对四种酯类与N_2的系统进行了高压相平衡研究。
本文运用自行设计的国内第一套带石英可视窗的可变体积高压釜,利用霍尔探测仪实现体积的准确测量,利用自动控温、恒温法和用手摇泵调节实现宽温度、压力范围的准确调控,用微型高压钢瓶实现高压状态直接取样,因此可方便地实现对高压气液平衡的准确测量。同时还建立了一套操作方便的组分解析装置,对气液相组成进行分析。采用静态分析法测定了一系列温度下N_2分别与碳酸二甲酯、碳酸二乙酯、乙酸乙酯、丙酸乙酯构成的二元系统的高压气液相平衡组成、相密度、体积。结果表明N_2在四种酯中溶解度随压力增加而明显增大,体现了相似相容的特性;但四种酯在气相中含量增加却不明显。其中N_2在碳酸酯系统中具有比饱和脂肪酸的酯相对较大的溶解度,且分子量越大、碳链越长,N_2的溶解度越低。而四种酯在N_2中的含量均很小,且相差不大。
选择PR和PRSV方程分别与Van der Waals-1型、Van der Waals-2型、Margules型混合规则和活度系数表达的混合规则搭配成八种不同的计算方法,采用搜索法对上述二元高压GLE实验数据进行优化计算,系统地分析了状态方程、混合规则、回归方法等对计算结果的影响。结果表明,PRSV方程与var der waals型混合规则组成的方法、PR方程与活度系数表达的混合规则组成的方法的计算效果均较好。
With the development of the research on phase equilibria, more phase equilibrium data of different systems are measured and calculated by using many methods. The content of nitrogen in the air is the most. However, the phase equilibria containing N_2 and ester are few. So the systems containing N_2 and four esters have been experimentally investigated and calculated.
A set of variable-volume autoclave with a quartz window has been made domestically for the first time. The accurate volume of a sample can be measured with a Hall-effect probe, and the precise adjustment within wide range of temperatures and pressures can be actualized. At high pressure, the samples can be taken directly from the autoclave with a small steel vessel. So the accurate vapor-liquid equilibrium data can be obtained. A simple equipment was also built up for the analysis the composition of the vapor and liquid samples. The vapor-liquid equilibrium data (including ingredient, density and volume) of the four binary systems (N_2+ dimethyl carbonate, N_2+diethyl carbonate, N_2+ ethyl acetate and N_2+ ethyl propionate) have been measured at different temperatures and pressures with isothermal static analytical method. The vapor-liquid equilibrium data show that the solubilities of N_2 in four esters increase drastically with increasing pressures at the given temperatures, but the contents of four esters in gas phases increase faintly. The solubilities of N_2 in the carbonate esters are higher than that in fatty acid esters, which reveals the principle that the similar structure makes the high solubility. And the higher the molecular weight is, the longer the carbon line is, the lower the solubility of N_2 is. However the contents of the four esters in N_2 are all low, and the differences among the contents are very little.
The high-pressure GLE data are also calculated with eight methods for above four systems. The PR and PRSV EOS and four different mixing rules are used. The Suitability of those EOSs and calculated precision are discussed systemically. Three methods showed excellent calculation effects which each other were made up of (PR EOS with activity coefficient and associated theory) and (PR EOS with var der waals mixing rules).
本文运用自行设计的国内第一套带石英可视窗的可变体积高压釜,利用霍尔探测仪实现体积的准确测量,利用自动控温、恒温法和用手摇泵调节实现宽温度、压力范围的准确调控,用微型高压钢瓶实现高压状态直接取样,因此可方便地实现对高压气液平衡的准确测量。同时还建立了一套操作方便的组分解析装置,对气液相组成进行分析。采用静态分析法测定了一系列温度下N_2分别与碳酸二甲酯、碳酸二乙酯、乙酸乙酯、丙酸乙酯构成的二元系统的高压气液相平衡组成、相密度、体积。结果表明N_2在四种酯中溶解度随压力增加而明显增大,体现了相似相容的特性;但四种酯在气相中含量增加却不明显。其中N_2在碳酸酯系统中具有比饱和脂肪酸的酯相对较大的溶解度,且分子量越大、碳链越长,N_2的溶解度越低。而四种酯在N_2中的含量均很小,且相差不大。
选择PR和PRSV方程分别与Van der Waals-1型、Van der Waals-2型、Margules型混合规则和活度系数表达的混合规则搭配成八种不同的计算方法,采用搜索法对上述二元高压GLE实验数据进行优化计算,系统地分析了状态方程、混合规则、回归方法等对计算结果的影响。结果表明,PRSV方程与var der waals型混合规则组成的方法、PR方程与活度系数表达的混合规则组成的方法的计算效果均较好。
With the development of the research on phase equilibria, more phase equilibrium data of different systems are measured and calculated by using many methods. The content of nitrogen in the air is the most. However, the phase equilibria containing N_2 and ester are few. So the systems containing N_2 and four esters have been experimentally investigated and calculated.
A set of variable-volume autoclave with a quartz window has been made domestically for the first time. The accurate volume of a sample can be measured with a Hall-effect probe, and the precise adjustment within wide range of temperatures and pressures can be actualized. At high pressure, the samples can be taken directly from the autoclave with a small steel vessel. So the accurate vapor-liquid equilibrium data can be obtained. A simple equipment was also built up for the analysis the composition of the vapor and liquid samples. The vapor-liquid equilibrium data (including ingredient, density and volume) of the four binary systems (N_2+ dimethyl carbonate, N_2+diethyl carbonate, N_2+ ethyl acetate and N_2+ ethyl propionate) have been measured at different temperatures and pressures with isothermal static analytical method. The vapor-liquid equilibrium data show that the solubilities of N_2 in four esters increase drastically with increasing pressures at the given temperatures, but the contents of four esters in gas phases increase faintly. The solubilities of N_2 in the carbonate esters are higher than that in fatty acid esters, which reveals the principle that the similar structure makes the high solubility. And the higher the molecular weight is, the longer the carbon line is, the lower the solubility of N_2 is. However the contents of the four esters in N_2 are all low, and the differences among the contents are very little.
The high-pressure GLE data are also calculated with eight methods for above four systems. The PR and PRSV EOS and four different mixing rules are used. The Suitability of those EOSs and calculated precision are discussed systemically. Three methods showed excellent calculation effects which each other were made up of (PR EOS with activity coefficient and associated theory) and (PR EOS with var der waals mixing rules).
引文
[1] 朱自强,徐汛,化工热力学,第二版,北京:化学工业出版社,1991,P188
[2] Christov M., Dohrn R., High-pressure fluid phase equilibria Experimental methods and systemsinvestigated (1994–1999), Fluid Phase Equilibria, 2002, 202: 153~218
[3] 朱自强,超临界流体技术-原理和应用,第一版,北京: 化学工业出版社,2003.:P517～538
[4] 朱自强,姚善泾,金彰礼等,流体相平衡原理及应用,浙江:浙江大学出版社,杭州:1990年.
[5] Hala E , Pick J, Fried V, et al., Vapour-Liquid Equilibrium, 2nd Eng. Ed., London: Pergamon Press, 1967. 147~148
[6] Marteau Ph, Tobaly P, Ruffier-Meray V, et al, in Situ Determination of High Pressure Phase Diagrams of Methane-Heavy Hydrocarbon Mixtures Using an Infrared Absorption Method, Fluid Phase Equilib., 1996,119:213~230
[7] Ebeling H, Frank E U, Ber. Bunsenges, Physi.Chem., 1984, 85:862
[8] Yonker C R, Linehan J C, Fulton J L, The Use of High Pressure NMR for the Determination of Phase Behavior for Select Binary Solvent Systems, J. Supercrit. Fluids, 1998,14:9~16.
[9] Brunner G. Gas Extraction. (Steinkopff, Darmstadt, Germany)New York: Springer,1994
[10] BüNz A P, Zitko-Stemberger N, Dohrn R, J. Supercrit. Fluids, 1994,7:43~50
[11] Schulze W, Vapor-Liquid Equilibria and Saturation Densities in the Ternary System Helium-Nitrogen-Methane, Fluid Phase Equilib. 1997,134:213~224
[12] Borch-Jensen Ch, Mollerup J, Phase Equilibria of Fish Oil in Sub- and Supercritical Carbon Dioxide, Fluid Phase Equilib., 1997,138:179~211
[13] Pfohl O Avramova, Brunner G, Two- Phase and Three-Phase Equilibria in Systems Containing Benzene Derivatives, Carbon Dioxide, and Water at 373.15 K and 10-30 Mpa, Fluid Phase Equilib., 1997,141:179~206
[14] Baba-Ahmed S, Guilbot P, Richon D, New Equipment Using a StaticAnalytic Method for the Study of Vapour–Liquid Equilibria at Temperatures down to 77 K, Fluid Phase Equilib., 1999,166:225~236
[15] Brunner G, Teich J, Dohrn R, Phase Equilibria in Systems Containing Hydrogen, Carbon Dioxide, Water and Hydrocarbons, Fluid Phase Equilib., 1994,100:253~268
[16] Kordikowski A, Schneider G M, Fluid Phase Equilibrium Studies on Ternary and Quaternary Mixtures of Carbon Dioxide with 1-Dodecanol, Dodecanoic Acid, Quinoxaline and 1,8-octanediol at 393.2 K and at Pressures up to 40 Mpa, Fluid Phase Equilib., 1995,105:129~139
[17] Pfohl O, Pagel A, Brunner G, Phase Equilibria in Systems Containing O-Cresol, P-Cresol, Carbon Dioxide, and Ethanol at 323.15–473.15 K and 10–35 Mpa, Fluid Phase Equilib., 1999,157:53~79
[18] Zaboloy M S, Gros H P, Bottini S B, et al, Isothermal Vapor-Liquid Equilibrium Data for the Binaries Isobutane-Ethanol, Isobutane-Propanol, and Propan-Ethanol, J. Chem. Eng. Data, 1994,39:214~218
[19] Deiters U K, Shneider G M, Fluid Phase Equbilirium,1986,29:145~160., Phase Equilibria of Liquid and Gaseous Mixtures at High-Pressures, In: Le Neindre B, Vodar B(Eds), Experimental Thermodynamics, Vol.Ⅱ,Part 2, Butterworth, London,1975, 787~801
[20] Camy S, Pic J S, Badens J S, et al, Fluid Phase Equilibria of the Reacting Mixture in the Dimethyl Carbonate Systhesis from Supercritical CO2, Journal of Supercritical Fluid, 2003,25:19~23.
[21] Costa M A M, Matos H A S, Nunes Da Ponte M, et al, Binary and Ternary Phase Behavior of A-Pinene, B-Pinene and Supercritical Ethene, J. Chem. Eng. Data, 1996,41:1104~1110
[22] Ewing M B, Sanchez Ochoa J C, an Ebulliometer for Measurements of Vapour Pressure at Low Temperatures: the Vapour Pressures and the Critical State of Perfluoromethylcyclopentane, J. Chem. Thermodyn., 1998,30:189~198
[23] Simnick J J, Lawson C C, Lin H M, et al, Vapor-Liquid Equilibrium of Hydrogen Tetralin System at Elevated Temperatures and Pressures, Aiche J. 1977, 23 :469
[24] Li Shufen, Varadarajan G S, Hartland S, Solubilities of the Obromine and Caffeine in Supercritical Carbon Dioxide: Corrlation with Density-Based Models, Fluid Phase Equilib., 1991, 68:263
[25] Jan D-S, Mai Ch-H, Tsai F-N, Solubilities of Carbon Dioxide in 1-Tetradecanol, 1- Hexadevanol and 1-Octadecanol, J. Chem. Eng. Data, 1994,39:384~387
[26] Mendes R L, Nobre B P, Coelho J P, et al, Solubility of Β-Carotene in Supercritical Carbon Dioxide and Ethane, J. Supercrit. Fluids, 1999,16:99~106
[27] Sovova H, Jez J, Khachaturyan M, Solubility of Squalane, Dinonyl Phthalate and Glycerol in Supercritical CO2, Fluid Phase Equilibrium, 1997,137:185~191
[28] Vandana V, Teja A.S, the Solubility of Paclitaxel in Supercritical CO2 and N2O, Fluid Phase Equilibrium, 1997,135:83~87
[29] Nagahama K, VLE Measurements at Elevated Pressures for Process Development, Fluid Phase Equilibrium, 1996,116:361~372
[30] 邱祖民,汽液相平衡测定的研究进展,江西科学,1996,14(4):254~257
[31] Chen A-Q, Urbanus G J, Chao K-Ch, A New Vapor-Liquid Equilibrium Cell and VLE Data for Mixtures of 1-propanol + p-xylene, Fluid Phase Equilibrium, 1994,94:281~288
[32] 田宜灵,韩铭,陈丽等,高压下 CO2-乙醇二元系统的气液平衡,物理化学学报,2001,17(2):155~160
[33] Schneider G M, Physicochemical Aspects of Fluid Extraction, Fulid Phase Equilibria, 1983,10:141~157
[34] Franck E U, Kerschbaum S, Wiegard G, The Density of Toluene at High Pressures to 673K and 300mpa, Ber. Bunsenges, Physi.Chem., 1998, 102(12): 1794~1797
[35] Schneider G M, High Pressure Thermodynamics of Mixtures, Pure Appl. Chem., 1976, 47: 277
[36] 胡英,物理化学,北京:人民教育出版社,1979
[37] Hubert C, Kriegel E, Application of supercritical gas extraction process on the food industry, Ger Chem Eng, 1984, 7: 335~341
[38] Jinglin Yu, Shujun Wang, Yiling Tian. Experimental Determination and Calculation of Thermodynamic Properties of CO2 + Octane to High Temperatures and High Pressures, Fluid Phase Equilibria, 2006, 246(1-2), 6-14.
[39] Yu Jinglin, Tian Yiling*, Zhu Rongjiao, High pressure Vapor-Liquid Equilibrium of Supercritical Carbon Dioxide+ n-hexane System. Journal of Tianjin University(Science and Technology), 2006, 12.
[40] Yu jinglin, Wang shujun, Tian yiling,Xu wei. Calculation of Critical Curves for Carbon Dioxide n-Alkane Systems. Trends in Applied Sciences Research. 2006,1(4):317-326.
[41] Tian Yiling, Chen Li, Li Mingwei, Fu Huafeng. Calculation of Gas-liquid Critical Curves for Carbon Dioxide-1-Alkanol, J. Phys. Chem. (in U.S.A.), 2003, 107(17): 3076~3080
[42] 朱虎刚,田宜灵,陈丽等,超临界 CO2+CH3OH 及 C2H5OH 二元系的气液平衡,高等学校化学学报,2002,3(8):1588～1592
[43] 田宜灵,韩铭,陈丽等,高压下 CO2-乙醇二元系统的气液平衡,物理化学学报,2001, 17(2):155～160
[44] Han Fang, Xue Yuan, Tian Yiling et al, Vapor-Liquid Equilibria of the Carbon Dioxide + Acetone System at Pressures from (2.36 to 11.77) MPa and Temperatures from (333.15 to 393.15) K, J. Chem. Eng. Data, 2005, 50(1): 36~39
[45] 赵雪峰,陈丽,田宜灵等,超临界 CO2+碳酸二乙酯二元体系高压气液相平衡,高等学校化学学报,2004,25(7): 1298~1302
[46] G. Brunner, R. Dohrn, High-Pressure Fluid-Phase Equilibria: Experimental Methods and Systems Investigated (1988-1993),Fluid Phase Equilibria, 1995, 106: 213~282
[47] Christov M., Dohrn R., High-pressure fluid phase equilibria Experimental methods and systemsinvestigated (1994–1999), Fluid Phase Equilibria, 2002, 202: 153~218
[48]朱自强,姚善泾,金彰礼,流体相平衡原理及其应用,浙江大学出版社,杭州:1990 年
[49] Kolasniska G, Moorwood R A S, Wenzel H G, Calculation of Vapor-Liquid and Liquid- Liquid Equilibrium by an Equation of State,Fluid Phase Equilibria, 1983, 13: 121
[50] Gibbons R M, Laughton A P, An Equation of State for Hydrochloric Acid Solutions, Fluid Phase Equilibria, 1984, 18: 61
[51] 李伯耿,骆有寿,朱自强,含盐溶液气液平衡的状态方程法研究—单一溶剂盐溶液蒸汽压的测定及关联,化工学报,1986,1:51
[52] Prausnitz J M, State-of-the-Art review of phase equilibria in phase equilibria and fluid propenties in the chemical industry, ACS Symposium Series, 60, ACS Washington, 1977, 11
[53] 武内胜彦,荒井康彦,状态方程开发的动向,化学工学,Symposium Series 2,化学工学协会,东京,1983,117
[54] 金克新,赵传钧,马沛生,化工热力学,天津:天津大学出版社,第二版,1992,P174
[55] Lentz, H., Zeuner, V. Phase diagrams of molar volume against mole fraction at given temperatures and pressures for {xAAr+xBXe+(1-xA-xB)NH3},J. Chem. Thermodynamics, 1995, 27: 997~1015.
[56] Weber W, Petkov S, Brunner G, Vapour–Liquid-Equilibria and Calculations Using the Redlich–Kwong-Aspen-Equation of State for Tristearin, Tripalmitin, and Triolein in CO2 and Propane, Fluid Phase Equilibrium, 1999,158~160:695~706
[57] 陈丽,含超临界 CO2 的二元系统高压相平衡和临界曲线:[博士学位论文],天津大学,2003.
[58] Prausnitz J M, Molecular Thermodynamics of Fluids, New Jersey, Englewood Cliffs: Prentice-hall, Inc., 1986, 446~447.
[59] Van Der Waals, Die Kontinuitat Des Gasformigen und Flussigen Zustandes. 2nd, Vol.1, Barth, Leipzig:1899~1900
[60] Redlich O, Kwong J N S, Chem Rer, 1949, 44:233
[61] Soave G, Equilibrium Constants from a Modified Redlich-Kwong Equation of State. Chem. Eng. Sci.1972, 27:1197
[62] Peng D Y, Robinson D B, A New Two-Constant Equation of State, Ind. Eng. Chem. Fundamentals, 1976,15:59～64
[63] Tsonopulos C, Heidma J I, from Redlich-Kwong to the Present, Fluid Phase Equilibria, 1985, 24:1
[64] Stryjek R, Vera J H, PRSV: An Improved Peng-Robinson Equation of State for Pure Compounds and Mixtures, Can. J. Chem. Eng., 1986,64:323～333
[65] Hong G T, Modell M, Tester J W, Binary Phase Diagrams from a Cubic Equation of State, Chemical Engineering at Supercritical Fluid Condition, Ann Atbot Science, Ann Atbot 1983:263
[66] Mart C J, Papadopoulos K D, Donohue M D, Application of Perturbed-Hard-Chain Theory to Solid-Supercritical Fluid Equilibria Modeling, Ind. Eng. Chem. Proc. Des. Dev. 1986, 25(2): 394
[67] Serbanovic S P, Djordjevic B O, Influence of the Optimized Temperature-Dependent Interaction Parameter on Vapor-Liquid Equilibrium Binary Predictions of Supercritical Methane with Some Alkanes By Means of the Soave Equation of State, Ind. Eng. Chem. Proc. Des., 1987, 26(3): 618
[68] 胡英,近代化工热力学,上海:上海科学技术文献出版社,1994,Chap.1~2
[69] Anderko A, Equation of State Methods for The Modeling of Phase Equilibria, Fluid Phase Equili., 1990,61:145
[70]朱自强。超临界流体萃取中的相平衡进展,高校化学工程学报,1994,8(1):1~10
[71] Soave G, Improvement of the Van Der Waals Equation of State, Chem. Eng. Sci., 1984,39:357
[72] Pl?cker U, Knapp H, Prausnitz J M, Estimation of Solvent Activities in Polymer Solutions Using a Group-Contribution Method, Ind. Eng. Chem. Proc. Des. Dev., 1978, 17:332
[73] Panagiotopoulos A Z, Reid A C, Watanasiri S, Multiphase High Pressure Equilibria in Ternary Aqueous Systems, Fluid Phase Equili., 1986, 29:525
[74] Stryjek R, Vera J H, PRSV: An Improved Peng-Robinson Equation With New Mixing Rules for Strongly Nonideal Mixtures, Can. J. Chem. Eng., 1986,64:323～333
[75] Schwartzen-Truber J, Galivel-Solastiouk F, Renon H, Fluid Phase Equili., 1987, 38:217
[76] Wilczek-Vera C, Vera J H, A Comparative Study of Mixing Rules forCubic Equations of State, Fluid Phase Equili., 1987, 37:241
[77]王东宇,李岳,王淑兰,R-K-S 方程在压缩因子计算中的应用,化学工业与工程技术,2001,22(5):32~35
[78] 徐南平,王延儒,时钧,高压流体相平衡的热力学理论—状态方程的回顾与展望,南京化工学院学报,1991,13(3):88~94
[79] 姚善泾,陈欢,朱自强,用状态方程计算含超临界二氧化碳体系的相平衡,浙江大学学报,1986,20(5):24
[80] Panagiotopoulos A Z, Reid R C, Equation of State Theories and Applications (Ed) Chao K C, Jr R L, Robinson, ACS Symposlum Series ,1986, 300:571
[81] 董军航,徐南平,王延儒等,改进的 PR 方程关联推算 N2-CH4-CO2体系高压汽液平衡,南京化工学院学报,1993,15(3):12
[82] Stryiek R, Vera J H, PRSV2:A Cubic Equation of State for Accurate Vapor-Liquid Equilibria Calculations. Can. J. Chem. Eng., 1986,64:820
[83] Twu C H, A Modified Redlich-Kwong Equation of State for Highly Polar Supercritical Systems, 1988,Proc of ISTCEI, Beijing: PR China,48~169
[84] 刘昆元,王文川,Peng-Robinson 状态方程计算含氢系统气液平衡-超临界气体的参数处理,化工学报,1989,1:73~81
[85] Huron M J, Vidal J, New Mixing Rules in Simple Equations of State for Epresenting Vapour-Liquid Equilibria of Strongly Non-Ideal Mixtures, Fluid Phase Equilibria, 1979, 3:255-271
[86] Renon H, Prausnitz J M, Local Compositions in Thermodynamic Excess Functions for Liquid Mixtures, Aiche J., 1968,14:135-144
[87] Stryjek R, Vera J H, PRSV2: A Cubic Equation of State for Accurate Vapor-Liquid Equilibria Calculations, Can. J. Chem. Eng., 1986,64:821-826
[88] 马沛生, 石油化工基础数据手册,续编, 北京:化学工业出版社,1993,1012
[89] Stryiek R, Vera J H, PRSV: An Improved Peng-Robinson Equation of State for Pure Compounds and Mixtures, Can. J. Chem. Eng., 1986, 64, 323~333
[2] Christov M., Dohrn R., High-pressure fluid phase equilibria Experimental methods and systemsinvestigated (1994–1999), Fluid Phase Equilibria, 2002, 202: 153~218
[3] 朱自强,超临界流体技术-原理和应用,第一版,北京: 化学工业出版社,2003.:P517～538
[4] 朱自强,姚善泾,金彰礼等,流体相平衡原理及应用,浙江:浙江大学出版社,杭州:1990年.
[5] Hala E , Pick J, Fried V, et al., Vapour-Liquid Equilibrium, 2nd Eng. Ed., London: Pergamon Press, 1967. 147~148
[6] Marteau Ph, Tobaly P, Ruffier-Meray V, et al, in Situ Determination of High Pressure Phase Diagrams of Methane-Heavy Hydrocarbon Mixtures Using an Infrared Absorption Method, Fluid Phase Equilib., 1996,119:213~230
[7] Ebeling H, Frank E U, Ber. Bunsenges, Physi.Chem., 1984, 85:862
[8] Yonker C R, Linehan J C, Fulton J L, The Use of High Pressure NMR for the Determination of Phase Behavior for Select Binary Solvent Systems, J. Supercrit. Fluids, 1998,14:9~16.
[9] Brunner G. Gas Extraction. (Steinkopff, Darmstadt, Germany)New York: Springer,1994
[10] BüNz A P, Zitko-Stemberger N, Dohrn R, J. Supercrit. Fluids, 1994,7:43~50
[11] Schulze W, Vapor-Liquid Equilibria and Saturation Densities in the Ternary System Helium-Nitrogen-Methane, Fluid Phase Equilib. 1997,134:213~224
[12] Borch-Jensen Ch, Mollerup J, Phase Equilibria of Fish Oil in Sub- and Supercritical Carbon Dioxide, Fluid Phase Equilib., 1997,138:179~211
[13] Pfohl O Avramova, Brunner G, Two- Phase and Three-Phase Equilibria in Systems Containing Benzene Derivatives, Carbon Dioxide, and Water at 373.15 K and 10-30 Mpa, Fluid Phase Equilib., 1997,141:179~206
[14] Baba-Ahmed S, Guilbot P, Richon D, New Equipment Using a StaticAnalytic Method for the Study of Vapour–Liquid Equilibria at Temperatures down to 77 K, Fluid Phase Equilib., 1999,166:225~236
[15] Brunner G, Teich J, Dohrn R, Phase Equilibria in Systems Containing Hydrogen, Carbon Dioxide, Water and Hydrocarbons, Fluid Phase Equilib., 1994,100:253~268
[16] Kordikowski A, Schneider G M, Fluid Phase Equilibrium Studies on Ternary and Quaternary Mixtures of Carbon Dioxide with 1-Dodecanol, Dodecanoic Acid, Quinoxaline and 1,8-octanediol at 393.2 K and at Pressures up to 40 Mpa, Fluid Phase Equilib., 1995,105:129~139
[17] Pfohl O, Pagel A, Brunner G, Phase Equilibria in Systems Containing O-Cresol, P-Cresol, Carbon Dioxide, and Ethanol at 323.15–473.15 K and 10–35 Mpa, Fluid Phase Equilib., 1999,157:53~79
[18] Zaboloy M S, Gros H P, Bottini S B, et al, Isothermal Vapor-Liquid Equilibrium Data for the Binaries Isobutane-Ethanol, Isobutane-Propanol, and Propan-Ethanol, J. Chem. Eng. Data, 1994,39:214~218
[19] Deiters U K, Shneider G M, Fluid Phase Equbilirium,1986,29:145~160., Phase Equilibria of Liquid and Gaseous Mixtures at High-Pressures, In: Le Neindre B, Vodar B(Eds), Experimental Thermodynamics, Vol.Ⅱ,Part 2, Butterworth, London,1975, 787~801
[20] Camy S, Pic J S, Badens J S, et al, Fluid Phase Equilibria of the Reacting Mixture in the Dimethyl Carbonate Systhesis from Supercritical CO2, Journal of Supercritical Fluid, 2003,25:19~23.
[21] Costa M A M, Matos H A S, Nunes Da Ponte M, et al, Binary and Ternary Phase Behavior of A-Pinene, B-Pinene and Supercritical Ethene, J. Chem. Eng. Data, 1996,41:1104~1110
[22] Ewing M B, Sanchez Ochoa J C, an Ebulliometer for Measurements of Vapour Pressure at Low Temperatures: the Vapour Pressures and the Critical State of Perfluoromethylcyclopentane, J. Chem. Thermodyn., 1998,30:189~198
[23] Simnick J J, Lawson C C, Lin H M, et al, Vapor-Liquid Equilibrium of Hydrogen Tetralin System at Elevated Temperatures and Pressures, Aiche J. 1977, 23 :469
[24] Li Shufen, Varadarajan G S, Hartland S, Solubilities of the Obromine and Caffeine in Supercritical Carbon Dioxide: Corrlation with Density-Based Models, Fluid Phase Equilib., 1991, 68:263
[25] Jan D-S, Mai Ch-H, Tsai F-N, Solubilities of Carbon Dioxide in 1-Tetradecanol, 1- Hexadevanol and 1-Octadecanol, J. Chem. Eng. Data, 1994,39:384~387
[26] Mendes R L, Nobre B P, Coelho J P, et al, Solubility of Β-Carotene in Supercritical Carbon Dioxide and Ethane, J. Supercrit. Fluids, 1999,16:99~106
[27] Sovova H, Jez J, Khachaturyan M, Solubility of Squalane, Dinonyl Phthalate and Glycerol in Supercritical CO2, Fluid Phase Equilibrium, 1997,137:185~191
[28] Vandana V, Teja A.S, the Solubility of Paclitaxel in Supercritical CO2 and N2O, Fluid Phase Equilibrium, 1997,135:83~87
[29] Nagahama K, VLE Measurements at Elevated Pressures for Process Development, Fluid Phase Equilibrium, 1996,116:361~372
[30] 邱祖民,汽液相平衡测定的研究进展,江西科学,1996,14(4):254~257
[31] Chen A-Q, Urbanus G J, Chao K-Ch, A New Vapor-Liquid Equilibrium Cell and VLE Data for Mixtures of 1-propanol + p-xylene, Fluid Phase Equilibrium, 1994,94:281~288
[32] 田宜灵,韩铭,陈丽等,高压下 CO2-乙醇二元系统的气液平衡,物理化学学报,2001,17(2):155~160
[33] Schneider G M, Physicochemical Aspects of Fluid Extraction, Fulid Phase Equilibria, 1983,10:141~157
[34] Franck E U, Kerschbaum S, Wiegard G, The Density of Toluene at High Pressures to 673K and 300mpa, Ber. Bunsenges, Physi.Chem., 1998, 102(12): 1794~1797
[35] Schneider G M, High Pressure Thermodynamics of Mixtures, Pure Appl. Chem., 1976, 47: 277
[36] 胡英,物理化学,北京:人民教育出版社,1979
[37] Hubert C, Kriegel E, Application of supercritical gas extraction process on the food industry, Ger Chem Eng, 1984, 7: 335~341
[38] Jinglin Yu, Shujun Wang, Yiling Tian. Experimental Determination and Calculation of Thermodynamic Properties of CO2 + Octane to High Temperatures and High Pressures, Fluid Phase Equilibria, 2006, 246(1-2), 6-14.
[39] Yu Jinglin, Tian Yiling*, Zhu Rongjiao, High pressure Vapor-Liquid Equilibrium of Supercritical Carbon Dioxide+ n-hexane System. Journal of Tianjin University(Science and Technology), 2006, 12.
[40] Yu jinglin, Wang shujun, Tian yiling,Xu wei. Calculation of Critical Curves for Carbon Dioxide n-Alkane Systems. Trends in Applied Sciences Research. 2006,1(4):317-326.
[41] Tian Yiling, Chen Li, Li Mingwei, Fu Huafeng. Calculation of Gas-liquid Critical Curves for Carbon Dioxide-1-Alkanol, J. Phys. Chem. (in U.S.A.), 2003, 107(17): 3076~3080
[42] 朱虎刚,田宜灵,陈丽等,超临界 CO2+CH3OH 及 C2H5OH 二元系的气液平衡,高等学校化学学报,2002,3(8):1588～1592
[43] 田宜灵,韩铭,陈丽等,高压下 CO2-乙醇二元系统的气液平衡,物理化学学报,2001, 17(2):155～160
[44] Han Fang, Xue Yuan, Tian Yiling et al, Vapor-Liquid Equilibria of the Carbon Dioxide + Acetone System at Pressures from (2.36 to 11.77) MPa and Temperatures from (333.15 to 393.15) K, J. Chem. Eng. Data, 2005, 50(1): 36~39
[45] 赵雪峰,陈丽,田宜灵等,超临界 CO2+碳酸二乙酯二元体系高压气液相平衡,高等学校化学学报,2004,25(7): 1298~1302
[46] G. Brunner, R. Dohrn, High-Pressure Fluid-Phase Equilibria: Experimental Methods and Systems Investigated (1988-1993),Fluid Phase Equilibria, 1995, 106: 213~282
[47] Christov M., Dohrn R., High-pressure fluid phase equilibria Experimental methods and systemsinvestigated (1994–1999), Fluid Phase Equilibria, 2002, 202: 153~218
[48]朱自强,姚善泾,金彰礼,流体相平衡原理及其应用,浙江大学出版社,杭州:1990 年
[49] Kolasniska G, Moorwood R A S, Wenzel H G, Calculation of Vapor-Liquid and Liquid- Liquid Equilibrium by an Equation of State,Fluid Phase Equilibria, 1983, 13: 121
[50] Gibbons R M, Laughton A P, An Equation of State for Hydrochloric Acid Solutions, Fluid Phase Equilibria, 1984, 18: 61
[51] 李伯耿,骆有寿,朱自强,含盐溶液气液平衡的状态方程法研究—单一溶剂盐溶液蒸汽压的测定及关联,化工学报,1986,1:51
[52] Prausnitz J M, State-of-the-Art review of phase equilibria in phase equilibria and fluid propenties in the chemical industry, ACS Symposium Series, 60, ACS Washington, 1977, 11
[53] 武内胜彦,荒井康彦,状态方程开发的动向,化学工学,Symposium Series 2,化学工学协会,东京,1983,117
[54] 金克新,赵传钧,马沛生,化工热力学,天津:天津大学出版社,第二版,1992,P174
[55] Lentz, H., Zeuner, V. Phase diagrams of molar volume against mole fraction at given temperatures and pressures for {xAAr+xBXe+(1-xA-xB)NH3},J. Chem. Thermodynamics, 1995, 27: 997~1015.
[56] Weber W, Petkov S, Brunner G, Vapour–Liquid-Equilibria and Calculations Using the Redlich–Kwong-Aspen-Equation of State for Tristearin, Tripalmitin, and Triolein in CO2 and Propane, Fluid Phase Equilibrium, 1999,158~160:695~706
[57] 陈丽,含超临界 CO2 的二元系统高压相平衡和临界曲线:[博士学位论文],天津大学,2003.
[58] Prausnitz J M, Molecular Thermodynamics of Fluids, New Jersey, Englewood Cliffs: Prentice-hall, Inc., 1986, 446~447.
[59] Van Der Waals, Die Kontinuitat Des Gasformigen und Flussigen Zustandes. 2nd, Vol.1, Barth, Leipzig:1899~1900
[60] Redlich O, Kwong J N S, Chem Rer, 1949, 44:233
[61] Soave G, Equilibrium Constants from a Modified Redlich-Kwong Equation of State. Chem. Eng. Sci.1972, 27:1197
[62] Peng D Y, Robinson D B, A New Two-Constant Equation of State, Ind. Eng. Chem. Fundamentals, 1976,15:59～64
[63] Tsonopulos C, Heidma J I, from Redlich-Kwong to the Present, Fluid Phase Equilibria, 1985, 24:1
[64] Stryjek R, Vera J H, PRSV: An Improved Peng-Robinson Equation of State for Pure Compounds and Mixtures, Can. J. Chem. Eng., 1986,64:323～333
[65] Hong G T, Modell M, Tester J W, Binary Phase Diagrams from a Cubic Equation of State, Chemical Engineering at Supercritical Fluid Condition, Ann Atbot Science, Ann Atbot 1983:263
[66] Mart C J, Papadopoulos K D, Donohue M D, Application of Perturbed-Hard-Chain Theory to Solid-Supercritical Fluid Equilibria Modeling, Ind. Eng. Chem. Proc. Des. Dev. 1986, 25(2): 394
[67] Serbanovic S P, Djordjevic B O, Influence of the Optimized Temperature-Dependent Interaction Parameter on Vapor-Liquid Equilibrium Binary Predictions of Supercritical Methane with Some Alkanes By Means of the Soave Equation of State, Ind. Eng. Chem. Proc. Des., 1987, 26(3): 618
[68] 胡英,近代化工热力学,上海:上海科学技术文献出版社,1994,Chap.1~2
[69] Anderko A, Equation of State Methods for The Modeling of Phase Equilibria, Fluid Phase Equili., 1990,61:145
[70]朱自强。超临界流体萃取中的相平衡进展,高校化学工程学报,1994,8(1):1~10
[71] Soave G, Improvement of the Van Der Waals Equation of State, Chem. Eng. Sci., 1984,39:357
[72] Pl?cker U, Knapp H, Prausnitz J M, Estimation of Solvent Activities in Polymer Solutions Using a Group-Contribution Method, Ind. Eng. Chem. Proc. Des. Dev., 1978, 17:332
[73] Panagiotopoulos A Z, Reid A C, Watanasiri S, Multiphase High Pressure Equilibria in Ternary Aqueous Systems, Fluid Phase Equili., 1986, 29:525
[74] Stryjek R, Vera J H, PRSV: An Improved Peng-Robinson Equation With New Mixing Rules for Strongly Nonideal Mixtures, Can. J. Chem. Eng., 1986,64:323～333
[75] Schwartzen-Truber J, Galivel-Solastiouk F, Renon H, Fluid Phase Equili., 1987, 38:217
[76] Wilczek-Vera C, Vera J H, A Comparative Study of Mixing Rules forCubic Equations of State, Fluid Phase Equili., 1987, 37:241
[77]王东宇,李岳,王淑兰,R-K-S 方程在压缩因子计算中的应用,化学工业与工程技术,2001,22(5):32~35
[78] 徐南平,王延儒,时钧,高压流体相平衡的热力学理论—状态方程的回顾与展望,南京化工学院学报,1991,13(3):88~94
[79] 姚善泾,陈欢,朱自强,用状态方程计算含超临界二氧化碳体系的相平衡,浙江大学学报,1986,20(5):24
[80] Panagiotopoulos A Z, Reid R C, Equation of State Theories and Applications (Ed) Chao K C, Jr R L, Robinson, ACS Symposlum Series ,1986, 300:571
[81] 董军航,徐南平,王延儒等,改进的 PR 方程关联推算 N2-CH4-CO2体系高压汽液平衡,南京化工学院学报,1993,15(3):12
[82] Stryiek R, Vera J H, PRSV2:A Cubic Equation of State for Accurate Vapor-Liquid Equilibria Calculations. Can. J. Chem. Eng., 1986,64:820
[83] Twu C H, A Modified Redlich-Kwong Equation of State for Highly Polar Supercritical Systems, 1988,Proc of ISTCEI, Beijing: PR China,48~169
[84] 刘昆元,王文川,Peng-Robinson 状态方程计算含氢系统气液平衡-超临界气体的参数处理,化工学报,1989,1:73~81
[85] Huron M J, Vidal J, New Mixing Rules in Simple Equations of State for Epresenting Vapour-Liquid Equilibria of Strongly Non-Ideal Mixtures, Fluid Phase Equilibria, 1979, 3:255-271
[86] Renon H, Prausnitz J M, Local Compositions in Thermodynamic Excess Functions for Liquid Mixtures, Aiche J., 1968,14:135-144
[87] Stryjek R, Vera J H, PRSV2: A Cubic Equation of State for Accurate Vapor-Liquid Equilibria Calculations, Can. J. Chem. Eng., 1986,64:821-826
[88] 马沛生, 石油化工基础数据手册,续编, 北京:化学工业出版社,1993,1012
[89] Stryiek R, Vera J H, PRSV: An Improved Peng-Robinson Equation of State for Pure Compounds and Mixtures, Can. J. Chem. Eng., 1986, 64, 323~333