对二甲苯＋环己烷及对二甲苯—二甲基亚砜的固液相平衡和…

测定了对二甲苯＋环己烷及对二甲苯＋二甲基亚砜体系（均为简单低共熔混合物）的固液平衡相图。计算出它们在３１３．１５Ｋ的过量吉布斯自由能。结果表明两体系对理想溶液均产生正偏差。     

乙腈-水的液液、固液相平衡和过量Gibbs自由能

测制了xCH~3CN+(1-x)H~2O的液液、固液平衡相图, 此系液液分层的简单低共熔混合物类相图。低共熔点温度为227.44K, 组成x=0.955。最高临界溶解温度为271.0K, 临界组成x=0.35, 临界指数n=2.64。两液相与冰的平衡温度为263.07K。计算出体系在263.07K的过量Gibbs自由能G~m^E, 液液分层时G~m^E的最大值为1174J·mol^-^1。     

间二甲苯＋对二甲苯二元系的固液相平衡

间二甲苯＋对二甲苯二元系的固液相平衡车冠全，古喜兰，云逢存（中山大学化学系，广州５１０２７５）混合二甲苯是石油化工的主要产品之一，年产３０万吨乙烯工程有混合二甲苯几万吨。邻、间、对二甲苯和乙苯大量用于制造聚酯纤维、改性聚酯纤维、聚酯树脂、不饱和聚酯树...     

正已醇-邻、间、对二甲苯二元系固液相平衡

Melting temperatures have been measured and the solid-liquid phase diagrams constructed for 1-hexanol＋o-xylene, 1-hexanol＋m-xylene and 1-hexanol＋p-xylene. They are simple eutectic systems. Excess mole Gibbs free energies were calculated at 298.15K, showing larger positive deviations from ideal-solution behavior. The largest values of GmE are 711、 650 and 800 J•mol-1 for {o-C6H4(CH3)2＋C6H13OH}、 {m-C6H4(CH3)2 ＋ C6H13OH} and {p-C6H4(CH3)2＋C6H13OH} respectively.     

吉布斯自由能的某些应用

吉布斯自由能的某些应用严宣中（北京大学化学系１００８７１）化学反应倾向取决于吉布斯自由能（凸Ｇ），后者是培变（凸Ｈ）及在一定温度下嫡变（Ｔ凸Ｓ）①综合判据，即面Ｇ一面Ｈ—Ｔ凸Ｓ。具体判据是：凸Ｇ＞０，正向非自发反应（逆反应为自发反应）；凸Ｇ—０，反应...     

吉布斯自由能的多功能性质探讨

在物理化学常用的热力学函数中,吉布斯自由能是一个用途最为广泛、最具有明确意义的热力学函数,它除了在特定条件下可作为过程与方向的判据外,还具有狭义化学势、最大非膨胀功和狭义表面自由能等功能。本文就吉布斯自由能的多功能特性展开讨论,并通过两个实例说明实际体系中ΔG的计算方法及用途,以帮助学生在物理化学学习过程中深入理解吉布斯自由能。     

Nd(NO_3)_3-HNO_3-H_2O体系的过量吉布斯自由能和Nd(NO_3)_3-HNO_3-H_2O-HDEHP-AMSCO体系水相中各组分活度系数的计算

我们简化了混合电解质溶液过量吉布斯自由能的Pitzer公式。用此简化公式并结合我们以往的工作计算了Nd(NO_3)_3-HNO_3-H_2O体系的过量吉布斯自由能和Nd(NO_3)_3-HNO_3-H_2O-HDEHP-AMSCO体系水相中各组分的活度系数,计算值与实验值均很接近。此工作为镧系金属萃取分离进行热力学分析提供了方便。     

胺-水二元系固液相平衡及其水合物

测定了水+三乙胺,+N,N-二甲基甲酰胺(DMF),+N,N-二甲基乙酰胺(DNA)的固液平衡相图,3个体系均有固体水合物形成,它们分别是不相合熔点水合物N(C_2H_5)_3·3H_2O、相合熔点水合物DMF·3H_2O,DMF·2H_2O,DMA·3H_2O和(DMA)_2·3H_2O.对水合物的形成进行了分析并与文献结果相比较.     

超额自由能型汽液相平衡混合规则

较全面地介绍了近几年来发展的各种典型的超额自由能型汽液相平衡混合规则。该类混合规则吸取了状态方程法和活度系数法在相平衡预测方面的优点,并将对于极性体系预测能力非常强的活度系数模型直接应用于状态方程法的相平衡预测中,实现了向高温区的良好外推和对超临界和亚临界组分的连续准确描述。依次发展的HV型、WS型和TC型三个大类的超额自由能型混合规则中,TC型混合规则的预测精确度要略高于HV型、WS型混合规则的预测精确度,而HV型、WS型混合规则的预测精确度大致相当。从发展的角度看,这些超额自由能型混合规则还要接受三元以上体系的汽液相平衡和液液相平衡预测的考验。另外,如何将超额自由能型混合规则扩展到多参数方程来提高相平衡预测精度,也是超额自由能型混合规则的一个值得关注的发展方向。     

苯酚+环己酮固液平衡的热力学计算

对苯酚+环己酮低温固液平衡体系,直接由相图和基本热力学数据,计算体系热力学性质。使用Gibbs-Duhem方程和四参量GE方程,在220.00～241.00K区间,计算了8个温度的两组元活度系数和GE方程,在241.00K,x2=0.5、GE=783.69J/mol,SE=97.11/(mol.K),HE=24186.69J/mol。241.00K相合熔点化合物的离解平衡ΔrGm=1982.93J/mol,ΔrHm=5753.241J/mol,ΔrSm=15.65J/(mol.K)。体系偏离于规则溶液模型。在化合物存在相区,离解反应的反应焓变和熵变均可视之为常量。液相区不会存在稳定的化合物。     

Excess Gibbs Energy of Mixing for Organic Carbonates from Fitting of Their Binary Phase Diagrams with Nonideal Solution Models

The excess Gibbs energies of mixing in the liquid state were evaluated for all the ten binary combinations of these five organic carbonates: ethylene carbonate (EC), propylene carbonate, dimethyl carbonate (DMC), ethyl methyl carbonate, and diethyl carbonate by fitting their measured binary phase diagrams with thermodynamic nonideal solution models based on the regular solution model. Using the results of these model fits, activity coefficients of the components in the solvent mixtures were calculated for the binary series containing EC and DMC as the common component, and the composition-averaged excess Gibbs energies of mixing were calculated by integrating the energy in the whole composition range for all the binaries. The results showed the excess Gibbs energy of mixing, and therefore the intermolecular forces, to be responsible for the changes in the phase diagrams, in the activity coefficients, and in the composition-averaged excess energy for the different binary solution combinations.     

C_8芳烃异构体+异丙醇体系在333.15K时的过量摩尔Gibbs自由能

采用CP-I型汽液平衡双循环釜,测定了333.15 K时乙苯+异丙醇、邻二甲苯+异丙醇、间二甲苯+异丙醇、对二甲苯+异丙醇四个体系的汽液平衡数据,计算了该温度下四个体系的过量摩尔Gibbs自由能,并对所测数据进行了恒温下热力学一致性检验。用Wilson方程关联了实验数据,拟合精度令人满意。     

甲酰胺溶剂中溶质间的过量Gibbs自由能相互作用参数

利用气液色谱方法测定了２９８．１５Ｋ时若干非电解质溶质在甲酰胺－乙酰胺、甲酰胺－尿素、甲酰胺－高氯酸钠固定液中的保留参数，采用ＭｃＭｉｌａａｎ－Ｍａｙｅｒ理论，将溶液热力学过量性质与溶液中粒子的对相互作用，参相互作用参数相联系，利用热力学方法求得了溶质的保留参数与Ｇｉｂｌｓ自由能相互作用参数的关系，并就溶质－溶质间的相互作用及溶剂性质的影响进行了讨论。     

四元系溶液中溶质间的Gibbs自由能相互作用参数的研究

用气液色谱法测定２９８．１５Ｋ下，有机溶质在尿素＋高氯酸钠＋甲酰胺固定液中的保留参数，用ＭｃＭｉｌｌａｎ－Ｍａｙｅｒ理论，将溶液的势力学过量性质与溶液中粒子间的对相互作用、三相互作用参数相联系，用热力学方法求得该四元体系中溶质的气液色谱保留参数与Ｇｉｂｂｓ自由能相互作用参数的联系，并就溶质间的相互作用及混合溶剂性质的影响进行了讨论。     

Excess Gibbs free energy and kinetics of grain growth of nanostructured silver

Samples of nanostructured silver were prepared by a mechanochemical technique and by electrodeposition. In the former, the microstructure was stabilized by intergranular cosegregation of Mg and O atoms. The excess Gibbs free energy of these samples was investigated by e.m.f. measurements at 453 K in a solid state electrochemical cell with AgI as a solid electrolyte. Electrodeposited pure silver samples had a labile microstructure even at 298 K. Their structural relaxation process was monitored in situ by chronopotentiometric measurements in an aqueous iodoargentate electrolyte. The time dependence of the e.m.f. could be quantitatively described by a parabolic law of grain growth without any adjustable parameter. Received: 13 January 2000 / Accepted: 8 February 2000     

Vapor-Liquid Equilibria in the Binary System Formed by Methyltertiarybutylether with Benzene at 490 and 709 mm Hg

Abstract

Isobaric vapor-liquid equilibria over the entire composition range are obtained from the measurement of the liquid phase composition versus boiling temperatures by means of a Swietoslawski type ebulliometer at 490 and 709 mm Hg for the methyl-tertiary-butylether(1) + benzene(2) system. The experimental composition (x) versus temperature (t) values could be represented well by both the Wilson and NRTL models. The optimum Wilson parameters have been used to calculate the excess Gibbs free energy.     

糖与非电解质在甲酰胺中相互作用的Gibbs自由能参数

用气液色谱法测定了298.15K时10个非电解质溶质在不同浓度甲酰胺糖(葡萄糖,果糖,蔗糖)溶液中的保留参数.依据McMillanMayer理论,求得非电解质溶质与糖间的Gibbs自由能相互作用参数g_ij和g_ijj.采用OkamotoWood的基团加合法,求得各基团的Gibbs自由能相互作用参数G_x,y,讨论了非电解质溶质与糖间的相互作用以及溶剂性质的影响.     

Vapour pressure and excess Gibbs energy of binary 1,2-dichloroethane + cyclohexanone,chloroform + cyclopentanone and chloroform + cyclohexanone mixtures at temperatures from 298.15 to 318.15 K

The vapour pressures of the binary systems 1,2-dichloroethane + cyclohexanone, chloroform + cyclopentanone and chloroform + cyclohexanone mixtures were measured at temperatures between 298.15 and 318.15 K. The vapour pressures vs. liquid phase composition data for three isotherms have been used to calculate the activity coefficients of the two components and the excess molar Gibbs energies, G^E, for these mixtures, using Barker's method. Redlich–Kister, Wilson, NRTL and UNIQUAC equations, taking into account the vapour phase imperfection in terms of the 2-nd virial coefficient, have represented the G^E values. No significant difference between G^E values obtained with these equations has been observed. Our data on vapour–liquid equilibria (VLE) and excess properties of the studied systems are examined in terms of the DISQUAC and modified UNIFAC (Dortmund) predictive group contributions models.     

Solid-Solute Phase Equilibria in Aqueous Solution. XI. Aqueous Solubility and Standard Gibbs Energy of Cadmium Carbonate

The solubilities of CdCO₃ (otavite) in aqueous NaClO₄ solutions have been investigated as a function of ionic strength (0.15 I/mol-kg^–1 5.35, 25°C) and temperature (25°C T 75°C, I = 1.00 mol-kg^–1). A new Chemsage optimization routine was employed to simultaneously evaluate solubility data from this work and other sources, as well as standard electrode potentials determined at different ionic strengths. With the Pitzer equations the solubility constants, , were extrapolated to infinite dilution resulting in log and the ternary ion-interaction parameters ^S_Na,Cd = 0.19 and at 25°C. In addition, the following set of thermodynamic quantities can be derived from the present solubility data for otavite: _f G = –674.2±0.6 kJ-mol^–1; _f H = –755.3±3.4 kJ-mol^–1; S = 93±10 J-mol^–1K^–1. However, the present solubility data are also consistent with a recent determination of the standard entropy of otavite which leads to a recommended set of thermodynamic quantities [_f G (CdCO₃) = –674.2±0.6; _f H (CdCO₃) = –752.1±0.6; S (CdCO₃) = 103.9±0.2].