水合物反应液中水活度系数模型研究进展

水合物反应液中水活度系数的计算对水合物相平衡特性的研究及水合物技术的应用具有重要意义。 通过调研大量的国内外资料,概括了Margules、Wilson、NRTL、UNIQUAC及UNIFAC活度系数方程及其关联式等模型及其应用,结果表明,Margules模型常用于二元体系活度系数的计算,但对高温高压体系条件下的溶液适用性较差;Wilson模型参数回归误差稍大且不适于溶质与离子不能完全互溶体系;UNIQUAC模型在含水或咪唑类离子反应液体系中误差较大;多元离子体系相平衡的研究中常选择NRTL模型;UNIFAC模型拟合效果较好,可实现较高浓度体系活度系数的精确计算,应用较广泛。 水活度关联方程参数拟合效果好,且准确度高,但在高温高压水合物反应液体系中的计算仍是一个技术难点,是今后的研究方向。     

预测对称与非对称体系活度系数的改进UNIFAC模型

采用“有效”体积参数代替体积参数修改了原始 UNIFAC模型的组合部分 ,可提高非对称体系的预测精度。推导了有效体积参数和原有体积参数之间的关系。改进的 UNIFAC模型 ,将新提出的组合部分与原模型的剩余部分结合 ,可较好的用于聚合物溶液和比原 UNIFAC模型更小或更大分子的非对称体系 ,也可用于仅含标准流体的体系。与 UNIFAC- FV模型相比较 ,新模型具有在计算时不需要其他的数据 ,尤其是液体的摩尔体积的优点 ,实际应用非常方便。作为比较对最近修改的另一个 UNIFAC模型进行了类似的计算。     

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。     

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。     

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.     

基于链端体积分数的聚合物溶液理论

提出“链端体积分数”的概念以克服Flory-Huggins(FH)理论中的平均场假设.将聚合物多链体系看成一条“间隔连续链”,使一些热力学量写成路径积分的形式.在聚合物/溶剂体系中,保留了FH理论的无热熵假设,把总熵分为两部分,建立了一个新的聚合物溶液理论.计算了聚苯乙烯/环己烷体系的FH相互作用参数和相分离曲线,并与实验数据和FH理论作了比较,结果表明,我们的理论结果比FH的理论结果有了很大的改进.     

高溶解性盐水体系热力学模型预测能力的比较研究Ⅰ∶二元体系

用原始Pitzer模型、扩展的Pitzer模型、Pitzer-Simonson-Clegg模型、S-MSA模型和BET模型分别对LiCl-H2O,LiBr-H2O,CaCl2-H2O,Mg(NO3)2-H2O,MnCl2-H2O和Mn(NO3)2-H2O等六种不同体系的热力学性质进行描述,考察了各种模型的预测能力.结果表明原始Pitzer模型不能准确描述高浓电解质溶液的性质;扩展的Pitzer模型虽然能较准确地描述某些体系高浓度的热力学性质,但预测能力不足;Pitzer-Simonson-Clegg模型对高浓盐水体系热力学性质具有一定的预测能力,但拟合参数所用的最大浓度与溶解度相差很大时,外推饱和点的热力学性质则会出现较大偏差;S-MSA模型虽然可以将拟合参数的浓度范围扩大到饱和,但没有外推能力,而且需要溶液的密度数据,这限制了该模型的广泛应用;BET模型对这六种体系均体现出很强的预测能力,预测结果准确,且模型参数少,物理意义明确,该模型可用于熔盐水化物相变储能材料的设计.     

高溶解性盐水体系热力学模型预测能力的比较研究I: 二元体系

用原始Pitzer模型、扩展的Pitzer模型、Pitzer-Simonson-Clegg模型、S-MSA模型和BET模型分别对LiCl-H2O, LiBr-H2O, CaCl2-H2O, Mg(NO3)2-H2O, MnCl2-H2O和Mn(NO3)2-H2O等六种不同体系的热力学性质进行描述, 考察了各种模型的预测能力. 结果表明原始Pitzer模型不能准确描述高浓电解质溶液的性质; 扩展的Pitzer模型虽然能较准确地描述某些体系高浓度的热力学性质, 但预测能力不足; Pitzer-Simonson-Clegg模型对高浓盐水体系热力学性质具有一定的预测能力, 但拟合参数所用的最大浓度与溶解度相差很大时, 外推饱和点的热力学性质则会出现较大偏差; S-MSA模型虽然可以将拟合参数的浓度范围扩大到饱和, 但没有外推能力, 而且需要溶液的密度数据, 这限制了该模型的广泛应用; BET模型对这六种体系均体现出很强的预测能力, 预测结果准确, 且模型参数少, 物理意义明确, 该模型可用于熔盐水化物相变储能材料的设计.     

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。     

高溶解性盐水体系热力学模型预测能力的比较研究Ⅰ：二元体系

用原始Pitzer模型、扩展的Pitzer模型、Pitzer-Simonson-Clegg模型、S-MSA模型和BET模型分别对LiCl-H2O,LiBr-H2O,CaCl2-H2O,Mg（NO3）2-H,O,MnCl2-H2O和Mn（NO3）2-H2O等六种不同体系的热力学性质进行描述,考察了各种模型的预测能力．结果表明原始Pitzer模型不能准确描述高浓电解质溶液的性质;扩展的Pitzer模型虽然能较准确地描述某些体系高浓度的热力学性质,但预测能力不足;Pitzer-Simonson-Clegg模型对高浓盐水体系热力学性质具有一定的预测能力,但拟合参数所用的最大浓度与溶解度相差很大时,外推饱和点的热力学性质则会出现较大偏差;S-MSA模型虽然可以将拟合参数的浓度范围扩大到饱和,但没有外推能力,而且需要溶液的密度数据,这限制了该模型的广泛应用：BET模型对这六种体系均体现出很强的预测能力,预测结果准确,且模型参数少,物理意义明确,该模型可用于熔盐水化物相变储能材料的设计．     

Interaction parameters for multi-component aromatic extraction with sulfolane

Aromatic extraction is an important operation in petrochemical processing. Design of an aromatic extractor requires the knowledge of multi-component liquid–liquid equilibrium (LLE) data. Such experimental LLE data are usually not available and therefore can be predicted using various activity coefficient models. These models require proper binary interaction parameters, which are not yet available for all aromatic extraction systems. Furthermore, the parameters available for most of the ternary systems are specific to that system only and cannot be used for other ternary or multi-component systems. An attempt has been made to obtain these parameters that are globally applicable. For this purpose, the parameter estimation procedure has been modified to estimate the parameters simultaneously for different systems involving common pairs. UINQUAC and UNIFAC models have been used for parameter estimation. The regressed parameters are shown to be applicable for the ternary as well as for the multi-component systems. It is observed that UNIQUAC parameters provide a better fit for ternary LLE data, whereas, as one moves towards the higher component systems (quaternary and quinary) the UNIFAC parameters, which are a measure of the group contributions, predict the LLE better. Effect of temperature on UNIQUAC binary interaction parameters has been studied and a linear dependence has been observed.     

Liquid-liquid equilibrium in ternary ionic liquid systems by UNIFAC: New volume, surface area and interaction parameters. Part II

Ionic liquids are potential solvents for liquid extraction processes; thermodynamic modeling of liquid-liquid equilibrium (LLE) data is essential for the optimization and operation of these processes. Therefore, ternary LLE data in systems involving ionic liquids have been investigated by several years. In most of the cases, the thermodynamic modeling of these systems has been made using the NRTL model; in some cases, the UNIQUAC model has also been used. The structural parameters of UNIQUAC for ionic liquids have been determined either by empirical correlations or, more recently, through quantum mechanics calculation. This work is a continuation of a recent paper, in which the structural group volume and area parameters for the group-contribution UNIFAC method have been calculated for five ionic liquids following the quantum mechanics approach. In order to optimize the molecular geometry and to calculate the area and volume, the Density Functional Theory (DFT) and the Polarizable Continuum Method (PCM) were used, respectively. The obtained parameters were used to correlate LLE data for fifteen ternary systems, totalizing 155 tie-lines. New interaction parameters were also estimated between the solvent and the ionic liquid functional groups. The results are very satisfactory, with root mean square deviations 0.0037 between experimental and calculated equilibrium mole fractions.     

Isobaric (vapour+liquid) equilibria data for the binary systems (toluene+acetic acid) and (toluene+methyl ethyl ketone) at atmospheric pressure

Isobaric vapour–liquid equilibrium data have been measured for the binary systems toluene (1) + acetic acid (2) and toluene (1) + methyl ethyl ketone (2) at atmospheric pressure. An all-glass Fischer–Labodest-type apparatus, capable of handling pressures from 0.25 to 400 kPa and temperatures up to 523.15 K was used. The data were correlated by means of the NRTL, UNIQUAC, WILSON models and the applied UNIFAC model with satisfactory results; the relevant parameters are given and results were tested with regard to thermodynamic consistency using the methods of a modified Redlich–Kister and Herington equations.     

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.     

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.     

Solubility of polycyclic aromatics in binary solvent mixtures using activity coefficient models

Polycyclic aromatic hydrocarbons (PAHs) precipitation is one of the major problems in the hydrocracking units. In this investigation, pyrene and phenanthrene were selected because they were found to be in higher concentrations in the feed to hydrocracking units. Their solubilities were investigated in toluene solvent mixture of iso-octane and heptane over a temperature range from 293 to 323 K. The experimental solubility data were used to predict the interaction parameters for seven different solid–liquid equilibrium models. The following activity coefficient models were used; Wilson, NIBS/Redlich–Kister, UNIQUAC, modified UNIFAC, modified UNIFAC (Dortmund), Flory–Huggins and Sheng. The interaction parameters were expressed as a second-order polynomial function in temperature. In order to test the models, the average absolute deviation percentage (AADP) was used. The overall AADP was found to range from approximately 7 to 14%. The models can be arranged according to their accuracy in a descending order based on AADP as follows: NIBS/Redlich–Kister, Wilson, UNIQUAC, Sheng, Flory–Huggins, modified UNIFAC (Dortmund) and finally modified UNIFAC. All models used in this work gave reasonable results; however, the group contribution models can also be used as a predictive tool for the solubility measurement of pyrene and phenanthrene in other solvents containing the same groups of the solvents used in this study.     

Isothermal vapor–liquid equilibria for mixtures composed of 1,2-dimethoxybenzene, 2-methoxyphenol,and diphenylmethane

Diphenylmethane was found to be a potential entrainer for separating the closely boiling mixtures of 2-methoxyphenol+1,2-dimethoxybenzene via extractive distillation. To gain insight into the capability of this auxiliary agent, isothermal vapor–liquid equilibrium data were measured for the binary and the ternary mixtures containing 2-methoxyphenol, 1,2-dimethoxybenzene, and diphenylmethane at temperatures from 433.15 to 463.15 K. All the binary data passed thermodynamic consistency tests. However, there exhibits a large discrepancy between the experimental values and the predicted results from the UNIFAC model. The new data were correlated with the Wilson, the NRTL, and the UNIQUAC models, respectively. The model parameters determined from the binary data were applied to predict the phase equilibrium behavior of the ternary system.