UNIFAC模型的在线参数优化——非电解质体系汽液相平衡数据库的应用

本文对基团贡献思想进行了探讨和进一步扩展,提出了基团贡献法模型在线参数优化的方法,并应用非电解质体系汽液相平衡数据库(NEDB),对UNIFAC 基团贡献法活度系数模型进行了在线参数优化的研究。22个体系的汽液平衡计算实例表明,在线参数优化的方法一般能使UNIFAC 模型对汽液平衡的预测精度有较为显著的提高。     

基于PSRK模型预测高分子溶液汽液平衡

为了更好地预测高分子溶液的汽液平衡,本文应用PSRK模型改进的混合规则[即将组合项(∑xiInb／bi)与原UNIFAC模型中的组合项(Flory-Huggins项)相抵消所获得的简化的混合规则]来计算方程的能量参数α。为了计入自由体积效应对高分子溶液的过量Gibbs自由能的贡献,在计算体积参bij时,将原混合规则中的指数修订为bij^1/2(bi^1/2 bj^1/2)/2。应用PSRK模型结合改进的混合规则预测二元高分子溶液体系的汽液平衡,结果表明新模型的计算精度是令人满意的。     

多元气-液-固复杂体系相平衡

石油流体中含有气相、液相及可能遇到的固相包括水合物、石蜡和沥青质等,涉及多元气-液-固复杂体系的相平衡问题.为防止这些沉积物堵塞造成安全隐患,需要确定水合物、石蜡、沥青质沉积起始条件以及沉积量.本文针对化学热力学理论在含水合物、石蜡和沥青质的多元-多相平衡研究中的应用进行了综述.水合物相平衡模型较为成熟,主要有两类,其一为基于等温吸附理论的van der Waals-Platteeuw型热力学模型;其二为基于双过程水合物生成机理的Chen-Guo水合物热力学模型.石蜡沉积一般采用活度系数法、状态方程法及多固相模型描述.沥青质絮凝、沉积则可采用溶解度参数模型、状态方程法、胶体模型和标度理论模型进行计算.同时对多元气-液-固复杂体系的相平衡研究发展方向进行了展望.     

White流体重整化群理论的标度性质

平均场状态方程结合重整化群理论的方法能预测流体的临界性质以及远离临界点的热力学性质. 利用经典的参数型状态方程结合White的重整化过程计算了CO2以及多种正构烷烃(C1～C7)的汽液相平衡热力学性质, 并在此基础上讨论了真实流体在临界点附近的非对称性质. 计算结果表明, White的流体重整化群理论能够很好地预测流体的相平衡热力学性质, 但是对于临界非对称性质不能给出与标度理论相符的结果.     

1,4-丁二醇蒸馏底物解聚溶液组成的分析方法

使用液液萃取法分析溶液中的1,4-丁二醇(BDO)含量,正辛醇作为萃取剂,在30 ℃下测定了水-BDO-正辛醇三元液液相平衡数据。 使用扩展型UNIQUAC模型建立了溶液中水-BDO-正辛醇的活度系数模型,关联该体系的液液平衡数据,通过单纯型法回归获得三元体系组分之间的相互作用能参数。 实验数据以及计算结果表明,通过分析萃取相的组成,能可靠地预测萃余相的组成,进而得到原溶液中BDO的含量。 该法准确、简便,可作为该体系的常规分析方法。     

用重整化群理论研究胶体模型体系的相行为

用yukawa势能函数表达胶体颗粒之间的吸引作用。用Duh-Mier-Y-Teran状态方 程表达液相Helmholtz自由能。用一阶微扰理论、固体硬球径向分布函数解析式和 改进的胞腔模型建立固相状态方程，结合建立的状态方程和重整化群理论。研究了 胶体模型体系的液-液相平衡和液-固相平衡。研究表明，颗粒之间色散作用量程参 数的变化对胶休到本世纪末茶杯 系的相行为有特殊需要影响。所得结果与分子模 拟数据吻合良好。     

磷酸三丁酯与醇二元混合体系的热力学性质

用量热法测定了298.15 K时, 磷酸三丁酯(TBP)+甲醇/乙醇/正丁醇/正丙醇四个二元混合体系的超额混合焓及293.15 K和303.15 K时部分组成下的超额混合焓, 其值均在−0.3 − 0.3 kJ•mol−1之间, 且基本不受温度的影响. 用无热溶液模型计算了各体系的超额熵、超额Gibbs自由能及各组分的活度系数. 热力学分析表明, TBP+甲醇/乙醇/正丙醇二元体系能较好地符合无热溶液模型, 而TBP+正丁醇体系则不符合无热溶液模型.     

二氧化碳和碳酸二甲酯二元体系的气液相平衡数据

实验测定了二氧化碳和碳酸二甲酯(DMC)二元体系的高压气液相平衡数据. 实验温度为333.0 到393.0 K, 实验压力为3.98 到13.75 MPa. 应用Peng-Robison (PR)立方形状态方程和van der Waals-1 混合规则对实验数据进行了关联计算, 同时得到了二元相互作用参数. 计算结果与实验数据具有很好的一致性.     

电动势法对LiCl-Li~2SO~4-H~2O体系25℃热力学性质研究

用自制的锂离子选择电极和经典Ag-AgCl电极,测定25℃时LiCl-Li~2SO~4-H~2O三元体系中离子强度0.01～6.0mol.kg^-1的LiCl平均活度系数.,由实验数据,用多元线性回归法求取Pitzer方程、Harned方程的离子作用参数和系数,并用上述方程计算LiCl在混合溶液中的平均活度系数,分别以Inγ~±LiCl和logγ~±LiCl的形式与实验值进行比较,标准偏差均小于0.008.本工作测得的LiCl平均活度系数的自然对数与等压法测定的渗透系数拟合的Pitzer方程参数计算值比较,标准偏差为0.0097.同时计算了Li~2SO~4在该体系中的平均活度系数和混合溶液的渗透系数以及混合超额自由能.     

DMF/水溶液中TDBAC与咪唑型离子液体混合胶束的聚集行为及热力学性质

利用电导法研究了298.15 K时十四烷基二甲基苄基氯化铵(TDBAC)与咪唑型离子液体表面活性剂Cn mim Br(n=12,16)混合胶束性质,考察了极性溶剂N,N-二甲基甲酰胺(DMF)对TDBAC/C16mim Br混合体系胶束化的影响。结果表明,混合体系在水溶液和DMF水溶液中都存在协同效应。随DMF体积分数的增加,TDBAC/C16mim Br混合体系临界胶束浓度(cmc)增大,而反离子结合度减小。利用胶束理论模型计算了混合胶束的组成、相互作用参数和活度系数,以及胶束形成混合自由能、混合熵和超额自由能等热力学函数。随DMF体积分数增加,协同作用下降,胶束形成的自发性降低。水溶液中混合胶束形成是焓效应与熵效应共同作用的结果,而在20%DMF水溶液中,胶束形成是熵驱动。     

Extension of Huron-Vidal-type Mixing Rule to Three-parameter Harmens-Knapp Cubic Equation of State

In this paper was extended the HV-type mixing rules to Harmens-Knapp cubic equation state (HK CEOS). The new HV-type mixing rule with HK CEOS was tested for Vapor-liquid equilibrium(VLE) of different polar and nonpolar systems. The tested results are in good agreement with existing experimental data within a wide range of temperatures and pressures. In comparison with the VDW mixing rule, the new mixing rule gives much better predictions for the VLE of nonpolar and polar systems.     

Development and extension of PSRK/UNIQUAC model to methane and nitrogen gases

Two successful procedures for matching the equation of state (EOS) and the excess Gibbs energy model at zero pressure belong to Michelsen [M.L. Michelsen, Fluid Phase Equilibria, 60 (1990) 213] and Holderbaum-Gmehling [T. Holderbaum, J. Gmehling, Fluid Phase Equilibria, 70 (1991) 251]. These procedures lead to volume independent mixing rules for the mixture parameter a. Michelsen proposed the MHV1 and MHV2 mixing rules and Holderbaum-Gmehling proposed the PSRK mixing rule. Keshtkar et al. [A. Keshtkar, F. Jalali, M. Moshfegian, Fluid Phase Equilibria, 140 (1997) 107] demonstrated the utility of these mixing rules together with UNIFAC and UNIQUAC models for the prediction of high-pressure vapor-liquid equilibrium (VLE) of CO₂-binary systems. Also, they showed that the PSRK/UNIQUAC model gives better VLE results than other models. In this paper, we develop and extend the above model to methane and nitrogen gases. For this purpose, it is required that the missing interaction parameters of model are fitted with experimental VLE data. The VLE calculations show that good agreement between calculated results and experimental data can be produced by using the obtained parameters.     

Vapor-liquid equilibria for benzyl alcohol with carbon dioxide, ethane, or nitrogen at elevated pressures

Vapor-liquid equilibrium (VLE) phase compositions were measured for the binary systems of benzyl alcohol with carbon dioxide, ethane, or nitrogen at temperatures from 333.15 K to 453.15 K and pressures up to 19 MPa. Henry's constants were calculated from the isothermal equilibrium data. The new VLE data were correlated by the Patel-Teja equations of state with three different types of mixing rules. In general, using the one-fluid, two-parameter van der Waals mixing rule yielded the best representation for the investigated systems. The validity of a generalized Soave model was also tested with the equilibrium data of carbon dioxide + benzyl alcohol.     

Examining the effect of binary interaction parameters on VLE modelling using cubic equations of state

Vapor-liquid equilibrium (VLE) data are important in the optimization of thermodynamic cycles. As energy concerns continue to grow, improving the efficiencies of power and refrigeration cycles is increasingly important. Numerical simulations using empirical equations of state provide an excellent alternative to time consuming experimental measurement of VLE data. However, it is important to understand the limitations of using correlative equations for data prediction. In this study, a water-ethanol mixture is simulated with various VLE models. Non-optimal binary interaction parameters are considered and model accuracy is evaluated in terms of average absolute percent deviation (%AAD) between simulated and experimental bubble and dew point pressures. For this system, it is found that as the correlative accuracy of a model increases, the predictive ability decreases. Specifically, the temperature dependence of the binary interaction parameters is shown to be an important consideration for the water-ethanol system when more complex combining rules are implemented.     

Application of a volume-translated Peng-Robinson equation of state on vapor-liquid equilibrium calculations

A volume-translated Peng-Robinson (VTPR) equation of state (EOS) is developed in this study. Besides the two parameters in the original Peng-Robinson equation of state, a volume correction term is employed in the VTPR EOS. In this equation, the temperature dependence of the EOS energy parameter was regressed by an improved expression which yields better correlation of pure-fluid vapor pressures. The volume correction parameter is also correlated as a function of the reduced temperature. The VTPR EOS includes two optimally fitted parameters for each pure fluid. These parameters are reported for over 100 nonpolar and polar components. The VTPR EOS shows satisfactory results in calculating the vapor pressures and both the saturated vapor and liquid molar volumes. In comparison with other commonly used cubic EOS, the VTPR EOS presents better results, especially for the saturated liquid molar volumes of polar systems. VLE calculations on fluid mixtures were also studied in this work. Traditional van der Waals one-fluid mixing rules and other mixing models using excess free energy equations were employed in the new EOS. The VTPR EOS is comparable to other EOS in VLE calculations with various mixing rules, but yields better predictions on the molar volumes of liquid mixtures.     

Effects of mixing rules on phase equilibrium calculations

The density dependence in the mixing rule of the cohesion parameter of the cubic equation of state is found not to be necessary in vapour—liquid equilibrium (VLE) calculations. The effects of the functional form and the number of the adjustable parameters of the mixing rules on VLE calculations are examined. It is found that the functional form is less influential in VLE calculations than the number of adjustable parameters and that two adjustable parameters in the mixing rules are sufficient for practical applications.     

Comparison of different mixing rules for prediction of density and residual internal energy of binary and ternary Lennard–Jones mixtures

Mixing rules are necessary when equations of state for pure fluids are used to calculate various thermodynamic properties of fluid mixtures. The well-known van der Waals one-fluid (vdW1) mixing rules are proved to be good ones and widely used in different equations of state. But vdW1 mixing rules are valid only when molecular size differences of components in a mixture are not very large. The vdW1 type density-dependent mixing rule proposed by Chen et al. [1] is superior for the prediction of pressure and vapor–liquid equilibria when components in the mixture have very different sizes. The extension of the mixing rule to chain-like molecules and heterosegment molecules was also made with good results. In this paper, the comparison of different mixing rules are carried out further for the prediction of the density and the residual internal energy for binary and ternary Lennard–Jones (LJ) mixtures with different molecular sizes and different molecular interaction energy parameters. The results show that the significant improvement for the prediction of densities is achieved with the new mixing rule [1], and that the modification of the mixing rule for the interaction energy parameter is also necessary for better prediction of the residual internal energy.     

Low pressure vapor–liquid equilibrium in ethanol + congener mixtures using the Wong–Sandler mixing rule

Phase equilibrium in binary ethanol mixtures found in alcoholic beverage production has been analyzed using a cubic equation of state (EoS) and suitable mixing and combining rules. The main objective of the study is the accurate modeling of the congener concentration in the vapor phase (substances different from ethanol), considered to be an important enological parameter in the alcohol industry. The Peng–Robinson (PR) equation of state has been used and the Wong–Sandler (WS) mixing rules, that include a model for the excess Gibbs free energy, have been incorporated into the equation of state constants. In the Wong–Sandler mixing rules the van Laar (VL) model for the excess Gibbs energy has been used. This combination of equations of state, mixing rules and combining rules are commonly applied to high pressure phase equilibrium and have not yet been treated in a systematic way to complex low pressure ethanol mixtures as done in this work. Nine binary ethanol + congener mixtures have been considered for analysis. Comparison with available literature data is done and the accuracy of the calculations is discussed, concluding that the model used is accurate enough for engineering applications.     

A new model and extension of Wong–Sandler mixing rule for prediction of (vapour + liquid) equilibrium of polymer solutions using EOS/GE

The cubic equation of state (CEOS) is a powerful method for calculation of (vapour + liquid) equilibrium (VLE) in polymer solutions. Using CEOS for both the vapour and liquid phases allows one to calculate the non-ideality of polymer solutions based on a single EOS approach. However, the traditional mixing rules are not appropriate to extend the CEOS to non-ideal mixtures such as polymer solutions. Several authors have applied the EOS/G^E approach to predict (vapour + liquid) equilibria in polymer solutions, however, incorporating an appropriate excess Gibbs free energy for the new mixing rule is a major step. In this research, the NRTL-NRF model was extended in terms of volume fraction of polymer and solvent (instead of mole fraction), then equilibrium calculations were carried out using PRSV EOS and Wong–Sandler mixing rules. Using the adjustable parameters as a function of solution temperature, the NRTL-NRF model can be used as a predictive model. In comparison with NRTL model, the results of the new NRTL-NRF model show better accuracy.