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。     

计算离子液体溶液汽液相平衡的分子热力学模型

用平均球近似理论、微扰理论和UNIFAC基团贡献方法分别考虑离子之间的长程静电作用、离子与溶剂之间的中程静电作用以及所有粒子之间的短程作用,本文提出了一种新的分子热力学模型,可用于离子液体溶液中溶剂活度系数的计算.通过对含烷基咪唑磷酸酯类离子液体与水、甲醇或乙醇组成的9个二元体系的饱和蒸汽压数据进行关联,获得了相关的模型参数,即溶剂的分子直径和基团之间的交互作用能参数.溶剂活度系数及饱和蒸汽压的计算结果与实验值的平均偏差为1.40%,符合良好,因此本模型可望用于含离子液体体系汽液相平衡的预测.     

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.     

聚合物溶液热力学模型的评述

预测聚合物溶液体系的气液平衡数据是热力学模型的一个重要内容.热力学模型大体可分3类,以过量吉布斯自由GF能表示的最为常用.本文选取基于GF的Flory-Huggins(FH)、UNIQUAC、UNIFAC和ENSIC 4种常用模型进行评述,认为FH模型出现较早,形式最简单;UNIQUAC模型发展较完善,应用范围较广,UNIFAC模型弥补了UNIQUAC模型参数缺乏的不足,应用最为;ENSIC模型具有较好的预测效果,但参数难以获得.     

水-环己酮-甲基异丁基酮液液相平衡数据的测定与关联

为了给以甲基异丁基酮为溶剂含环己酮废水萃取过程的设计和流程模拟计算提供数据支撑,本文测定了常压下,水+环己酮+甲基异丁基酮（MIBK）三元体系在303.15、313.15及323.15 K的液液相平衡数据。据相平衡数据计算了分配系数和分离因子,所有的分离因子均远大于1,表明MIBK从水中萃取环己酮是可行的;Hand方程和Bachman方程的相关系数在0.99以上,表明实验数据具有较好的一致可靠性。同时,采用NRTL和UNIQUAC活度状态方程对实验数据进行了关联,回归得到了该三元物系的二元交互参数,结果表明两种模型均能很好关联实验数据,实验值和模拟值的相对均方根差（RMSD）低于0.5%。     

气液色谱法研究聚合物/溶剂体系气液平衡

 用气液色谱法测定了聚二甲基硅氧烷（PDMS）／溶剂、聚甲基丙烯酸甲酯（PMMA）／溶剂体系在不同温度下以质量分数表示的无限稀溶剂活度系数和Flory－Huggins相互作用参数。应用UNIFAC和UNIFAC－FV模型对PDMS／溶剂、PMMA／溶剂体系中以质量分数表示的无限稀溶剂活度系数进行了估算。结果表明,用这两个模型预测PDMS／溶剂、PMMA／溶剂体系中的无限稀溶剂活度系数有待修正或采用其它模型进行估算。     

气液色谱法研究聚合物/溶剂体系气液平衡

用气液色谱法测定了聚二甲基硅氧烷（PDMS）／溶剂、聚甲基丙烯酸甲酯（PMMA）／溶剂体系在不同温度下以质量分数表示的无限稀溶剂活度系数和Flory－Huggins相互作用参数。应用UNIFAC和UNIFAC－FV模型对PDMS／溶剂、PMMA／溶剂体系中以质量分数表示的无限稀溶剂活度系数进行了估算。结果表明,用这两个模型预测PDMS／溶剂、PMMA／溶剂体系中的无限稀溶剂活度系数有待修正或采用其它模型进行估算。     

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。     

UNIFAC方程用于H2O—n—C12H26—D2EHPA—LaCl3—HCl萃取体系

本文实验测定了n-C_(12)H_(26)-D_2EHPA在盐酸介质中萃取La~(3+)的平衡数据和H_2O-n-C_(12)H_(26)D_2EHPA体系的活度系数.用Pitzer方程计算水相中H_2O和H~+、La~(3+)的活度系数,用UNIFAC方程计算有机相各组分的活度系数,提出了萃取剂和金属萃合物的基因划分方法,经数据拟合,获得了能在全浓度范围内适用的萃取反应平衡常数和UNIFAC参数,用这些参数成功计算了n-C_(12)H_(26)-D_2EHPA萃取La~(3+)的平衡浓度.     

丙烯腈、己二腈和丙腈与水的二元体系液-液相平衡数据的测定和关联(英文)

采用平衡法测定了丙烯腈+水、己二腈+水、丙腈+水三个二元体系在不同温度(303.15、313.15、323.15、333.15K)下的液-液相平衡数据;并采用NRTL(α=0.2,α=0.3)模型和UNIQUAC模型对液-液平衡数据进行了关联.结果显示,NRTL和UNIQUAC模型对三个二元体系在不同温度下的互溶度关联的目标函数值均小于1×10-17,实验值与计算值吻合较好,绝对偏差小于0.009,关联精度较高.该研究结果可为丙烯腈、丙腈和水三元平衡溶解度数据的模拟和预测提供可靠的基础数据,并对电解二聚法生产己二腈中电解液的分离提纯工艺具有一定的指导意义.     

Interpreting freezing point depression of stearic acid and methyl stearate

Freezing point depressions of binary systems including either stearic acid (SA) or methyl stearate (MES) were evaluated based on differential scanning calorimetry melting scans. The second binary component included a solvent from the group acetic acid, acetone, 2-butanone, and hexane. Vapor pressure as a function of liquid composition and temperature was used to measure vapor/liquid equilibrium. Activity coefficients were calculated from this data and models fit to the data to determine how well the models fit the solid–liquid equilibrium models.The Gibbs/Duhem equation and polymorphism of the melt transitions indicated that freezing point depressions were due to a combination of: (1) a reduction of activity of the triglyceride derivative in solution albeit with activity coefficients > 1.0, (2) incorporation of the solvent into the solid matrix for at least some of the mixtures, and (3) substantially different physical properties between the solid and liquid phases of the SA and MES. Different melting phenomena were observed in differential scanning calorimetry (DSC) scans depending upon the heteroatom functionality of the solvent.The empirical Margules, NRTL, and Wilson activity coefficient models fit data for the solvent activity coefficients well, while the UNIQUAC model combined with the predictive abilities of UNIFAC could not accurately predict activity coefficients. Despite questions on the fundamental interpretation of the data, modeling the activity coefficients for the solvent is sufficient to approximate the effect the solvent will have on the melting point depression. Relatively simple experiments following the total pressure of mixtures as a function of composition and temperature can be used to obtain activity coefficient model parameters for the Margules, NRTL, UNIQUAC, and Wilson.     

Experimental investigation of the vapour–liquid equilibrium of binary and ternary mixtures containing dibutyl ether (DBE), cyclohexane and toluene at 313.15 K

New vapour–liquid equilibrium data for binary and ternary mixtures formed by dibutyl ether (DBE), toluene and cyclohexane at 313.15 K have been measured. A static method using an isothermal total pressure cell (Van Ness’ technique) has been employed. The systems studied presented a slight deviation from ideal behaviour. None of them show azeotrope. The VLE data have been satisfactorily correlated with the equations of Margules, Wilson, NRTL and UNIQUAC for binaries and Wohl expansion, Wilson, NRTL and UNIQUAC for the ternary system. Predictions with UNIFAC group contribution methods are included.     

Vapor–liquid equilibrium of octane-enhancing additives in gasolines: 6. Total pressure data and GE for binary and ternary mixtures containing 1,1-dimethylethyl methyl ether (MTBE), methanol and n-hexane at 313.15 K

Experimental isothermal P–x data at T=313.15 K for the binary systems 1,1-dimethylethyl methyl ether (MTBE)+n-hexane and methanol+n-hexane, and the ternary system MTBE+methanol+n-hexane are reported. Data reduction by Barker’s method provides correlations for G^E using the Margules equation for the binary systems and the Wohl expansion for the ternary system. Wilson, NRTL and UNIQUAC models have been applied successfully to both the binary and the ternary systems. Moreover, we compare the experimental results for these binary mixtures to the prediction of the UNIFAC (Dortmund) model. Experimental results have been compared to predictions for the ternary system obtained from the Wilson, NRTL, UNIQUAC and UNIFAC models; for the ternary system, the UNIFAC predictions seem poor. The presence of azeotropes in the binary systems has been studied.     

Boiling points for five binary systems of sulfolane with aromatic hydrocarbons at 101.33 kPa

Boiling points have been determined at 101.33 kPa for the binary mixtures of sulfolane+o-xylene, sulfolane+m-xylene, sulfolane+p-xylene, sulfolane+ethylbenzene and sulfolane+1,2,4-trimethylbenzene. Calculations of the non-ideality of the vapor phase were made with the second virial coefficients evaluated from the Hayden–O’Connell method. The binary parameters for five activity coefficient models (Margules, van Laar, Wilson, NRTL and UNIQUAC) have been fitted with the experimental boiling points measured in this work. A comparison of model performances has been carried out using the criterion of the average absolute deviations in boiling point. The activity coefficient of the component in the liquid phase is discussed based on the UNIFAC model with the consideration of the dipole–dipole interactions.     

(Vapour + liquid) equilibrium of binary mixtures (1,3-dioxolane or 1,4-dioxane + 2-methyl-1-propanol or 2-methyl-2-propanol) at isobaric conditions

Isobaric (vapour + liquid) equilibrium of (1,3-dioxolane or 1,4-dioxane + 2-methyl-1-propanol or 2-methyl-2-propanol) at 40.0 kPa and 101.3 kPa has been studied with a dynamic recirculating still. The experimental VLE data are thermodynamically consistent. From these data, activity coefficients were calculated and correlated with the Margules, van Laar, Wilson, NRTL and UNIQUAC equations. The VLE results have been compared with the predictions by the UNIFAC and ASOG methods.     

Vapor-Liquid Equilibria in the Systems Ethyl 1,1-Dimethylethyl Ether + Cyclohexane and + Benzene at 94.00 kPa

Abstract

Consistent vapor-liquid equilibria for the binary systems of ETBE with benzene and cyclohexane at 94.00 kPa have been measured. Both systems show slightly positive deviation from ideal behavior and do no present azeotropic behavior. The activity coefficients and boiling points of the solutions were correlated with its mole fractions by the Redlich-Kister, Wohl, Wilson, UNIQUAC, NRTL, and Wisniak -Tamir equations. The data were also compared with UNIFAC predictions.     

Isobaric Vapour-Liquid Equilibrium of Some Cyclic Ethers with Bromobenzene at Several Pressures

A dynamic recirculating still was employed to study the isobaric vapour-liquid equilibrium (VLE) at 40.0 and 101.3 kPa for the binary systems tetrahydrofuran, tetrahydropyran, 2-methyl-tetrahydrofuran and 2,5-dimethyl-tetrahydrofuran with bromobenzene. The experimental data were tested for thermodynamic consistency and correlated with the Wilson, NRTL and UNIQUAC equations. Predictions with the UNIFAC method were also obtained.     

Phase equilibria in the ternary system ethyl 1,1-dimethylethyl ether+heptane+octane

Vapor–liquid equilibrium at 94 kPa has been determined for the ternary system ethyl 1,1-dimethylethyl ether (ETBE)+heptane+octane. The system deviates slightly from ideality and no azeotrope is present. The ternary activity coefficients and the boiling points of the system have been correlated with the composition using the Redlich–Kister, Wilson, NRTL, UNIQUAC, UNIFAC, and Wisniak–Tamir relations. Most of the models allow a very good prediction of the activity coefficients of the ternary system from those of the pertinent binary systems.     

Vapor–liquid equilibria for binary mixtures containing ethyl tert butyl ether (ETBE) + (p-xylene,m-xylene and ethylbenzene) at 101.3 kPa

Isobaric vapor–liquid equilibria data at 101.3?kPa were reported for the binary mixtures ethyl tert butyl ether (ETBE)?+?(p-xylene, m-xylene and ethylbenzene). VLE experimental data were tested for thermodynamic consistency by means of a modified Dechema test and was demonstrated to be consistent. The activity coefficients were correlated with the Margules, van Laar, UNIQUAC, NRTL, and Wilson equations. The Analytical Solution Of Groups (ASOG) model also was applied for prediction.     

Liquid–liquid phase equilibrium of methanol + ethylbenzene + isooctane + ethanol system at 303 K

The phase equilibrium data for methanol + ethanol + isooctane systems were obtained at 303.15 K. Data for methanol + ethylbenzene + isooctane system were taken from literature. The effect of ethanol addition on the system equilibrium was investigated at the same temperature. The distribution curves for ternary and quaternary system was analyzed. The experimental results for ternary systems were correlated with UNIQUAC and NRTL equations. For the ternary systems studied here, the NRTL equation is more accurate than the UNIQUAC. The equilibrium data for the three ternary systems were used to determine interactions parameters for the UNIQUAC equation. For the quaternary system, the experimental data can be fitted more accurately to UNIQUAC equation than by the UNIFAC method.