LCVM型混合规则扩展用于多参数状态方程以关联混合物汽液相平衡Extending LCVM-type Mixing Rule to Multi-parameter Equations of State for Vapor-liquid Equilibria of Mixtures
韩晓红,陈光明,王勤
摘要(Abstract):
基于两参数状态方程提出的LCVM混合规则是将以无穷压力为参考态的HV混合规则与以零压力为参考态的MHV1混合规则线性结合而得的,尽管没有理论基础,但对于计算非极性、极性体系给出了较好的结果。因而研究借鉴获得LCVM混合规则的思路将LCVM混合规则扩展到多参数状态方程中,即将HVOS混合规则与MHV1混合规则进行线性结合,并通过引入两个对比参数λ0,λ∞给出了适合多常数状态方程的新LCVM型混合规则。在新的LCVM型混合规则中,参数δ决定了MHV1和HVOS混合规则的相对贡献,该参数可由模型在高压和低压下拟合二元混合物的泡露点得到,通过拟合得到的值约为0.21;混合规则中的活度系数模型可以利用由低压区关联出的GE模型。采用该新混合规则模型,在较宽的温度与压力范围内,结合Harmens-Knapp(HK)方程对包括非极性体系、极性体系等在内的20种二元混合物进行了相平衡计算。计算的结果与实验数据吻合得很好。该模型与采用VDW混合规则模型的相平衡计算结果比较表明,该模型的关联精度有了很大的提高,可以在较大的温度与压力范围内关联多种体系的汽液相平衡数据。但是在混合规则中,参数b,c是依赖于经验获得,因此还有待于进一步的研究。
关键词(KeyWords): 汽液相平衡;状态方程;混合规则;活度系数
基金项目(Foundation): 浙江省自然科学基金资助项目(Z105034)
作者(Author): 韩晓红,陈光明,王勤
参考文献(References):
- [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 modified HV mixing rule for cubic equations of state[J].Fluid Phase Equilibria,1990,60:213-219.
- [3]Orbey H,Sandler S I.On the combination of EOS and free energy models[J].Fluid Phase Equilibria,1995,111:53-70.
- [4]Holderbaum T,Gmehling J.PSRK:a group contribution equation of state based on UNFIAC[J].Fluid Phase Equilibria,1991,70:251-265.
- [5]Boulouvalas C,Spiliotis N,et al.Prediction of vapor-liquid equilibrium 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.
- [6]Yang T,Chen G J,et al.Extension of the Wong-Sandler mixing rule to the three-parameter Patel-Teja equation of State:Application up to the near-critical region[J].Chemical Engineering Journal,1997,67:27-36.
- [7]Stabley M W.Phase Equilibria in Chemical Engineering[M].Beijing:China petro.Publishing company,1991.68-69.
- [8]Twu C H,Coon J E,Bluck D,Tilton B,Rowland M.Connection between zero-pressure mixing rules and infinite-pressure mixing rules[J].Fluid Phase Equilibria,1998,153:29-44.
- [9]Renon H,Prausnitz J M.Local composition in thermodynamic excess function for liquid mixture[J].AIChE J,1968,14:135-144.
- [10]HUANG Rong-rong(黄荣荣),YANG Ji-he,et al(杨基和等).Phase equilibrium in ternary system with carbondioxide,water,and acetic acid at high pressure(CO2-H2O-HAc三组分系统高压相平衡)[J].J Chem Eng of Chinese Univ(高校化学工程学报),2003,17(3):330-334.
- [11]Lim J S,Park J Y,Lee B G.Phase equilibria of1,1,1-trifluoroethane(HFC-143a)+1,1,1,2-tetrafluoroethane(HFC-134a),and+1,1-difluoro-ethane(HFC-152a)at273.15,293.15,303.15,313.15K[J].Fluid Phase Equilibria,2002,193:29-39.
- [12]Niesen V,Palavra A,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.
- [13]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.
- [14]Mitsuho H,Shuzo O,Kunio N.Computer Aided Data Book of Vapor-liquid Equilibria[M].Amsterdam and American:Elsevier Publishing Company,1986.
- [15]Lee M J,Hsiao C C,Lin H M.Isothermal vapor-liquid equilibria for mixtures of methyl tert-butyl ether,methyl acetate,and ethyl acetate[J].Fluid Phase Equilibria,1997,137:193-207.
- [16]Kagan B b,Fulideman B M,Kafalafu B B,Guangshui P T(version).Vapor-liquid Equilibria Database[M].Tokyo:Jiangtan Society Publishing Company,1974.
- [17]Coquelet C,Hong D N,et al.Vapour-liquid equilibrium data for the difluoromethane+1,1,1,2,3,3,3-heptafluoroprane system at temperatures from283.2to343.38K and pressures up to4.5MPa[J].International Journal of Refrigeration,2003,26:559-565.