Measurement of activity coefficients at infinite dilution in N-methyl-2-pyrrolidone and N-formylmorpholine and their mixtures with water using the dilutor technique

With the help of the dilutor technique activity coefficients at infinite dilution have been measured for 24 solutes (alkanes, alkenes, cyclic hydrocarbons, aromatic hydrocarbons, ketones, ethers and alcohols) in N-methyl-2-pyrrolidone (NMP), N-formylmorpholine (NFM) and their mixtures with water in the temperature range between 303.15 and 333.15 K (in a few cases for temperatures up to 423.15 K). The influence of water on the activity coefficient at infinite dilution is presented for different solutes. Furthermore, the selectivities at infinite dilution (S_ij^∞=γ_i^∞/γ_j^∞) for the separation of aliphatics from aromatics are discussed.     

The determination of activity coefficients at infinite dilution using g.l.c. for hydrocarbons in furfural at T=278.15 K and T=298.15 K

The activity coefficients at infinite dilution for some alkanes, cycloalkanes, alkenes, alkynes and benzene in furfural have been determined by g.l.c. at T=278.15 K and T=298.15 K. The volatility of the solvent furfural, although low, was taken into account. The method used is an alternative to the pre-saturation method. The results have been used to predict the potential for furfural as a solvent in separating aromatic compounds from aliphatic compounds and other hydrocarbons using extractive distillation. The excess enthalpies of mixing at infinite dilution have also been calculated.     

Extension of the A-UNIFAC model to mixtures of cross- and self-associating compounds

In the present work an extended UNIFAC group contribution model is used to calculate activity coefficients in solutions containing alcohols, water, carboxylic acids, esters, alkanes and aromatic hydrocarbons. The limiting expressions for the association contribution to the activity coefficients at infinite dilution are presented and discussed. A new set of interaction parameters between associating and non-associating functional groups is reported. This set of parameters is applied in the association model to predict vapor–liquid, liquid–liquid equilibrium and infinite dilution activity coefficients.     

Prediction of infinite dilution activity coefficients for systems including water based on the group contribution model with mixture-type groups: II. Extension and application

Group contribution models such as ASOG or UNIFAC were known to be inaccurate in the prediction of infinite dilution activity coefficients (γ^∞) for most of the systems containing water. To overcome the weakness inherent with the UNIFAC models, Zhang et al. (Fluid Phase Equil. 149 (1998) 27) have recently proposed a group-contribution-based model with mixture-type groups, where the mixture-type group is a hypothetical concept for taking into account the particular hydrophobic effects in aqueous organic systems. The proposed methodology has been proven to be applicable to alkane/water and alcohol/water mixtures in our previous study. In this work, the proposed method was further extended to the other classes of compounds, e.g. aromatics, ketones, acids, aldehydes, esters, ethers, nitriles and halogenated compounds. Compared to the conventional UNIFAC models, the proposed method demonstrates significant improvements in accuracy for various organic compounds in water mixtures.     

Henry’s law constants and infinite dilution activity coefficients of cis-2-butene,dimethylether, chloroethane,and 1,1-difluoroethane in methanol, 1-propanol, 2-propanol, 1-butanol, 2-butanol,isobutanol, tert-butanol, 1-pentanol, 2-pentanol, 3-pentanol, 2-methyl-1-butanol, 3-methyl-1-butanol,and 2-methyl-2-butanol

Henry’s law constants and infinite dilution activity coefficients of cis-2-butene, dimethylether, chloroethane, and 1,1-difluoroethane in methanol, 1-propanol, 2-propanol, 1-butanol, 2-butanol, isobutanol, tert-butanol, 1-pentanol, 2-pentanol, 3-pentanol, 2-methyl-1-butanol, 3-methyl-1-butanol, and 2-methyl-2-butanol in the temperature range of 250 K to 330 K were measured by a gas stripping method and partial molar excess enthalpies were calculated from the activity coefficients. A rigorous formula for evaluating the Henry’s law constants from the gas stripping measurements was used for the data reduction of these highly volatile mixtures. The uncertainty is about 2% for the Henry’s law constants and 3% for the estimated infinite dilution activity coefficients. In the evaluation of the infinite dilution activity coefficients, the nonideality of the solute such as the fugacity coefficient and Poynting correction factor cannot be neglected, especially at higher temperatures. The estimated uncertainty of the infinite dilution activity coefficients includes 1% for nonideality.     

Activity coefficients of hydrocarbon solutes at infinite dilution in the ionic liquid, 1-methyl-3-octyl-imidazolium chloride from gas–liquid chromatography

Activity coefficients for hydrocarbon solutes at infinite dilution in 1-methyl-3-octyl-imidazolium chloride have been measured using the medium pressure gas–liquid chromatography method. The hydrocarbon solutes used were n-pentane, n-hexane, n-heptane, n-octane, 1-hexene, 1-heptene, 1-octene, 1-hexyne, 1-heptyne, 1-octyne, cyclopentane, cyclohexane, cycloheptane, benzene, and toluene. Activity coefficients at infinite dilution were determined at the following three temperatures (298.15, 308.15, and 318.15) K. Selectivities for benzene and the hydrocarbons are presented and the results indicate that 1-methyl-3-octyl-imidazolium chloride is a reasonable solvent for the separation of an alkane or an alkene from benzene.     

Correlation and comparison of the infinite dilution activity coefficients in aqueous and organic mixtures from a modified excess Gibbs energy model

Activity coefficients at infinite dilution (ln γ^∞) of aqueous systems were calculated using a modified excess Gibbs energy model. More than 95 binary systems with 15 solute families from nonpolar alkanes to polar alcohols and acids were employed in this study. Based on the local composition lattice model developed by Aranovich and Donohue, a modified excess Gibbs energy equation (m-AD model) was derived in this study. With two generalized parameters for each homologous series of solutes, this modified model yields satisfactory results for the limiting activity coefficients. The overall absolute average deviation (AAD) of ln γ^∞ for all aqueous systems investigated in this study is 2% for the m-AD model, and the corresponding AAD in γ^∞ unit is 7%. The calculated infinite dilution activity coefficients from the m-AD model are comparable to those from the MOSCED, SPACE, PDD, LSER or the modified UNIFAC model. The m-AD model shows lower peak deviation than those from other methods. Satisfactory generalized correlation results are also observed for organic solvents other than water. With the generalized parameters, the m-AD model satisfactorily predicts the limiting activity coefficients for other solutes not included in the correlation.     

Infinite dilution activity coefficient and vapour liquid equilibrium measurements for dimethylsulphide and tetrahydrothiophene with hydrocarbons

The activity coefficients at infinite dilution (γ^∞) of dimethylsulphide (DMS) in four hydrocarbon solvents were measured using the dilutor technique at temperatures between 288 K and 303 K. The four hydrocarbons were hexane, 1-hexene, 2,2,4-trimethylpentane and 2,4,4-trimethyl-1-pentene. The dilutor technique is based on the stripping of the highly diluted solute, i.e. DMS, by a constant flow of inert gas. The gas composition was analysed by gas chromatography and the rate of solute removal was calculated from the area of the peaks.     

Henry’s constants and infinite dilution activity coefficients of propane,propene, butane,isobutene, 1-butene,isobutane, trans-2-butene and 1,3-butadiene in 1-propanol at T=(260 to 340) K

The Henry’s constants and the infinite dilution activity coefficients of propane, propene, butane, isobutane, 1-butene, isobutene, trans-2-butene and 1,3-butadiene in 1-propanol at T=(260 to 340) K are measured by a gas stripping method. The rigorous formula for evaluating the Henry’s constants from the gas stripping measurements is used for these highly volatile mixtures. The accuracy of the measurements is about 2% for Henry’s constants and 3% for the estimated infinite dilution activity coefficients. In the evaluations for the infinite dilution activity coefficients, the nonideality of solute is not negligible especially at higher temperatures and the estimated uncertainty in the infinite dilution activity coefficients include 1% for nonideality.