本文在假定AEOS∞≈[GE/(RT))]EOSp->0=[GE(x)/(RT)]solution model的基础上经过一系列的推导,将原WS混合规则中的交叉相互作用参数kij简化为一个只与组份和活度系数模型参数有关的函数,并将该简化后的WS混合规则(WS-S)结合PR状态方程及NRTL活度模型对16对双元混合物的汽液相平衡进行了关联.关联结果表明,在较宽的温度与压力范围内,应用该模型可得到令人满意的结果.与原WS混合规则相比,精度基本相当,但是计算量却得到了一定的减小,并使方程具有一定的预测性,可以更加方便地应用于工程设计计算中.
参考文献
[1] | Huron M;Vidal J .New Mixing Rules in Simple Equations of State for Representing Vapor-Liquid Equilibria of Strongly Nonideal Mixtures[J].Fluid Phase Equilibria,1979,3:225-271. |
[2] | Michelsen M L .A Method for Incorporating Excess Gibbs Energy Models in Equations of State[J].Fluid Phase Equilibria,1990,60:47-58. |
[3] | Michelsen M L .A Modified Huron-Vidal Mixing Rule for Cubic Equations of State[J].Fluid Phase Equilibria,1990,60:213-219. |
[4] | Holderbaum T;Gmehling J .PSRK:a Group Contribution Equation of State Based on UNFIAC[J].Fluid Phase Equilibria,1991,70:251-265. |
[5] | Orbey H.;Sandler SI. .ON THE COMBINATION OF EQUATION OF STATE AND EXCESS FREE ENERGY MODELS[J].Fluid Phase Equilibria,1995(1):53-70. |
[6] | Boulouvalas C;Spiliotis N;Coutsikos P et al.Prediction of Vapor-Liquid Equilibria with LCVM Model.A Linear Combination of the Huron-Vidal and Michelsen Mixing Rules Coupled with the Original UNIFAC and the t-Mpr Equation of state[J].Fluid Phase Equilibria,1994,92:75-106. |
[7] | David S H W;Sandler S I .A Theoretically Correct Mixing Rule for Cubic Equations of State[J].AICHE Journal,1992,38:671-680. |
[8] | Philippos C;Nikolaos S K;Dimitrios P T .Capabilities and Limitation of the Wong-Sandler Mixing Rules[J].Fluid Phase Equilibria,1995,108:59-78. |
[9] | Renon H;Prausnitz G.M .Local Compositions in Thermodynamic Excess Functions for Liquid Mixtures[J].AICHE Journal,1968,14(135):135-144. |
[10] | Mitsuho H;Shuzo O;Kunio N.Computer Aided Data Book of Vapor-Liquid Equilibria[M].Amsterdam and American Elsevier Publishing Company,1986 |
[11] | Kagan B B;Fulideman B M;Kafalafu B B.VaporLiquid Equilibria Database[M].Jiang Tan Society Publishing Company,1974 |
[12] | Sergio B;Roman S;Nicola E;Alberto B .A Recirculation apparatus for Vapor-Liquid Equilibrium Measurements of Refrigerants.Binary Mixtures of R600a,R134a,R236fa[J].Fluid Phase Equilibria,1998,150-151:343-352. |
[13] | Lee MJ.;Lin HM.;Hsiao CC. .ISOTHERMAL VAPOR-LIQUID EQUILIBRIA FOR MIXTURES OF METHYL TERT-BUTYL ETHER, METHYL ACETATE, AND ETHYL ACETATE[J].Fluid Phase Equilibria,1997(1/2):193-207. |
[14] | Lim JS.;Park JY.;Lee BG.;Lee YW. .Phase equilibria of 1,1,1-trifluoroethane (HFC-143a)+1,1,1,2-tetrafluoroethane (HFC-134a), and +1,1-difluoroethane (HFC-152a) at 273.15, 293.15, 303.15, and 313.15 K[J].Fluid Phase Equilibria,2002(1/2):29-39. |
[15] | Niesen V;Palavra A;Kidnay A J et al.An apparatus for Vapor-Liquid Equilibrium at Elevated Temperatures and Pressures and Selected Results and Pressures and selection Results for water-ethanol and Methanol-Ethanol Systems[J].Fluid Phase Equilibria,1986,31:283-298. |
[16] | Coquelet C;Nguyen H D;Chareton A et al.Vapor-liquid Equilibrium Data for the Difluoro-Methane+1,1,1,2,3,3,3-Heptafluoroprane System at Temperatures from 283.2 to 343.38 K and Pressures up to 4.5 MPa[J].International Journal of Refrigeration-Revue Internationale du Froid,2003,26:559-565. |
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