A method for measuring infinite-dilution partition coefficients of volatile compounds between the gas and liquid phases of aqueous systems

Vejrosta, J., Novák, J. and Jönsson, J.Å., 1982. A method for measuring infinite-dilution partition coefficients of volatile compounds between the gas and liquid phases of aqueous systems. Fluid Phase Equilibria, 8: 25–35.A method has been developed for measuring the partition coefficients of volatile compounds between the gas and liquid phases of aqueous systems, based on the direct analysis of both phases. A gas mixture containing a known proportion of a volatile compound is drawn through the liquid (water) until equilibrium is established. A defined volume of the liquid phase is then withdrawn through a porous-polymer trap while maintaining the system at equilibrium. The residual water in the trap is then expelled by a stream of nitrogen gas, and the deposit remaining is thermally desorbed and analyzed by gas chromatography. This approach, together with an experimental technique for producing gas mixtures containing an accurately known concentration of hydrocarbon at low values, makes it possible to determine accurately the partition coefficients of low-solubility compounds, such as for hydrocarbons in aqueous systems, at very low solute concentrations in the system. The method has been verified by measuring the partition coefficient of hexane between the gas and liquid phases of an aqueous system at various concentrations and temperatures.     

Vapor — liquid and vapor — liquid — liquid phase equilibria of binary and ternary systems of nitrogen,ethene and methanol: Experiment and data evaluation

Zeck, S. and Knapp, H., 1986. Vapor—liquid and vapor—liquid—liquid phase equilibria of binary and ternary systems of nitrogen, ethene and methanol: experiment and data evaluation. Fluid Phase Equilibria, 26: 37–58.VLE and VLLE of three binary and one ternary system containing the components N₂, C₂H₄ and CH₃OH are investigated in a high-pressure phase equilibrium apparatus with vapor recirculation at temperatures 240 < T < 298 K and pressures 4 < p < 100 bar. Immiscibilities in the liquid phase are observed in the binary system C₂H₄CH₃OH with a lower critical end point and in the ternary system N₂C₂H₄CH₃OH.The experimental results are reported and compared with the results of other investigators and of available correlations.     

Phase equilibria for the system Mn0.394Ti0.606OS at 1380 and 1485°K

This paper reports equilibrium phase data for the manganese-containing system Mn_0.394Ti_0.606OS. The system was studied at 1380 and 1485°K by an equilibration and quench technique. The oxygen and sulfur fugacities of the equilibrating gas atmosphere were independently controlled using mixtures of the three gases hydrogen, carbon dioxide, and hydrogen sulfide. The results are presented on log f_S2 vs log f_O2 phase diagrams which are discussed in terms of the equilibria between manganese in the oxide phases and manganese in the α-MnS sulfide phase. The results are shown to be consistent with previously published data for the subsystems MnTiO, MnOS, MnS, and TiOS.     

Pulsed NMR investigation of the supercooled water-gas hydrate-gas metastable equilibrium

A method is developed for determining the thermobaric conditions of phase equilibrium in a liquid water-hydrate-gas system by means of pulsed 1H NMR. The method is founded on NMR-based measurements of the amount of liquid water phase in a sample containing gas hydrate under certain values of pressure p and temperature T. The results from investigating the p,T conditions for metastable equilibrium in a supercooled water-Freon-12 hydrate-gas system are presented. The results are in good agreement with the known literature data.     

Vapor—liquid and vapor—liquid—liquid phase equilibria for binary and ternary systems for nitrogen,ethane and methanol: Experiment and data reduction

Zeck, S. and Knapp, H., 1986. Vapor-liquid and vapor-liquid-liquid phase equilibria for binary and ternary systems of nitrogen, ethane and methanol; experiment and data reduction. Fluid Phase Equilibria, 25: 302–322.VLE and VLLE are investigated for three binary and one ternary system containing N₂, C₂H₆ and CH₃OH in a high-pressure phase equilibrium apparatus with vapor recirculation at temperatures 240 < T < 298 K and pressures 4 < p < 75 bar. Two liquid phases are observed in the systems C₂H₆CH₃OH and N₂CH₃OH. Experimental results are reported and compared with available correlations.     

Liquid—vapor equilibrium in the system H2Ar at temperatures from 83 to 141 K and pressures to 52 MPa

Calado, J.C.G. and Streett, W.B., 1979. Liquid—vapor equilibrium in the system H₂Ar at temperatures from 83 to 141 K and pressures to 52 MPa. Fluid Phase Equilibria, 2: 275–282.Experimental measurements of liquid—vapor phase equilibria in the system H₂Ar are reported for thirteen temperatures in the range 83.09 to 141.42 K, and pressures to 52 MPa. The mixture critical line and the pressure—temperature trace of the three-phase line solid—liquid—gas have been located. These lines intersect at T = 84.0 K and P = 52.5 MPa to form an upper critical end point. The pressure—temperature trace of the three-phase line has a temperature minimum at T ? 82.5 K, P ? 20 MPa.     

Multiphase equilibria for binary and ternary mixtures containing propionic acid,n-butanol,butyl propionate,and water

Isothermal vapor–liquid equilibrium (VLE) data were measured for propionic acid + butyl propionate at 373.15 and 393.15 K, and isothermal vapor–liquid–liquid equilibrium (VLLE) data were also measured for n-butanol + water, butyl propionate + water, and water + n-butanol + butyl propionate at temperatures ranging from 323.15 to 393.15 K. No azeotrope was found in propionic acid + butyl propionate. The mutual solubility data of the binary aqueous systems were correlated well with the NRTL model accompanying with temperature-dependent parameters. Improvement on the calculation of saturated vapor compositions has been made by using two-term virial equation with one adjustable binary interaction parameter to represent the non-ideality of the vapor phase. The model parameters determined from the binary VLLE data of n-butanol + water and butyl propionate + water and the binary VLE data of n-butanol + butyl propionate are capable of predicting satisfactorily the VLLE properties for the ternary system of water + n-butanol + butyl propionate.     

水—正己烷—甲醇体系的液液平衡研究

随着国民经济的发展 ,汽油、柴油等发动机燃料的供求关系会日趋紧张 ,寻求代用燃料是今后燃料工业发展的必然趋势 ,而以甲醇、乙醇等作为部分代用燃料成分是今后的一个重要方向[1] 。由于传统的甲醇合成工艺受到传热、传质和化学平衡的限制 ,原料及能源的利用率有待于进一步提高。钟炳等人根据超临界相反应特点 ,向体系中加入适宜溶剂如正己烷 ,在超临界条件下合成甲醇 ,同时克服了现有过程存在的热力学限制和传热限制 ,并将ＣＯ单程转化率提高到 90 %以上[2 ] 。但是 ,正己烷的加入给合成甲醇过程带来了产物分离和溶剂回收问题。反应器流出…     

Measurements of methane hydrate equilibrium in systems inhibited with NaCl and methanol

Natural gas hydrates are ice-like inclusion compounds that form at high pressures and low temperatures in the presence of water and light hydrocarbons. Hydrate formation conditions are favorable in gas and oil pipelines, and their formation threatens gas and oil production. Thermodynamic hydrate inhibitors (THIs) are chemicals (e.g., methanol, monoethylene glycol) deployed in gas pipelines to depress the equilibrium temperature required for hydrate formation. This work presents a novel application of a stepwise differential scanning calorimeter (DSC) measurement to accurately determine the methane hydrate phase boundary in the presence of THIs. The scheme is first validated on a model (ice + salt water) system, and then generalized to measure hydrate equilibrium temperatures for pure systems and 0.035 mass fraction NaCl solutions diluted to 0, 0.05, 0.10, and 0.20 mass fraction methanol. The hydrate equilibrium temperatures are measured at methane pressures from (7.0 to 20.0) MPa. The measured equilibrium temperatures are compared to values computed by the predictive hydrate equilibrium tool CSMGem.     

Raman linewidth study of intermolecular interactions of methanol in aqueous solution

Isotropic Raman linewidths of the CH and CD symmetric stretching modes of methanol and methanol-d₄ have been measured as a function of concentration in normal water, in heavy water and in carbon tetrachloride. On the basis of the concentration dependence of observed linewidths, intermolecular interactions and liquid structures in the methanol—water system are discussed. It is suggested that there may be some difference in mutual affinities or abilities of hydrogen bonding in the order D₂O > H₂O > CD₃OD > CH₃OH.     

(Liquid + liquid) equilibria for ternary mixtures of (methanol or ethanol + toluene or m-xylene + n-dodecane)

(Liquid + liquid) equilibrium (LLE) results for the ternary mixtures of (methanol or ethanol + toluene or m-xylene + n-dodecane) at three temperatures (298.15, 303.15 and 313.15) K are reported. The compositions of liquid phases at equilibrium were determined by g.l.c. measurements and the results were correlated with the UNIQUAC and NRTL activity coefficient models. The partition coefficients and the selectivity factor of methanol and ethanol are calculated and compared to suggest which alcohol is more suitable for extracting the aromatic hydrocarbons (toluene or m-xylene) from n-dodecane. The phase diagrams for the ternary mixtures including both the experimental and correlated tie lines are presented. From the phase diagrams and the selectivity factors it is concluded that methanol has a higher efficiency as a solvent in extraction of aromatic hydrocarbon from alkane mixtures.     

Development of a new equation of state for mixed salt and mixed solvent systems,and application to vapour–liquid and solid (hydrate)–vapour–liquid equilibrium calculations

An equation of state that can be used for phase equilibrium and other thermodynamic property calculations at high pressures is developed for systems that contain aqueous solutions of strong electrolytes and molecular species. The proposed equation of state is based upon contributions to the Helmholtz free energy from a non-electrolyte term and three electrolyte terms. The non-electrolyte term comes from the Trebble–Bishnoi equation of state and the electrolyte terms consist of a Born energy term, a mean spherical approximation term and a newly developed hydration term. The application of the proposed equation of state to aqueous systems containing mixed salts and mixed solvents is illustrated by calculating the vapour–liquid equilibrium (VLE) and solid (Clathrate hydrate)–vapour–liquid equilibrium (SVLE) conditions for several systems. The solubility of CO₂ in salt water systems is examined at elevated pressures. As well, the new equation of state is used in conjunction with the model of van der Waals and Platteeuw to predict the SVLE conditions for gas hydrate forming systems in the presence of single salts, mixed salts and a mixture of aqueous salts and methanol. It is found that the new equation of state is able to accurately represent the experimental data over a wide range of pressure, temperature and salt concentration.     

Vapor–liquid equilibrium of systems containing alcohols,water, carbon dioxide and hydrocarbons using SAFT

The statistical associating fluid theory (SAFT) equation of state is employed for the correlation and prediction of vapor–liquid equilibrium (VLE) of eighteen binary mixtures. These include water with methane, ethane, propane, butane, propylene, carbon dioxide, methanol, ethanol and ethylene glycol (EG), ethanol with ethane, propane, butane and propylene, methanol with methane, ethane and carbon dioxide and finally EG with methane and ethane. Moreover, vapor–liquid equilibrium for nine ternary systems was predicted. The systems are water/ethanol/alkane (ethane, propane, butane), water/ethanol/propylene, water/methanol/carbon dioxide, water/methanol/methane, water/methanol/ethane, water/EG/methane and water/EG/ethane. The results were found to be in satisfactory agreement with the experimental data except for the water/methanol/methane system for which the root mean square deviations for pressure were 60–68% when the methanol concentration in the liquid phase was 60 wt.%.     

Aqueous solubility calculation for petroleum mixtures in soil using comprehensive two-dimensional gas chromatography analysis data

An assessment of aqueous solubility (leaching potential) of soil contaminations with petroleum hydrocarbons (TPH) is important in the context of the evaluation of (migration) risks and soil/groundwater remediation. Field measurements using monitoring wells often overestimate real TPH concentrations in case of presence of pure oil in the screened interval of the well. This paper presents a method to calculate TPH equilibrium concentrations in groundwater using soil analysis by high-performance liquid chromatography followed by comprehensive two-dimensional gas chromatography (HPLC-GCXGC). The oil in the soil sample is divided into 79 defined hydrocarbon fractions on two GCXGC color plots. To each of these fractions a representative water solubility is assigned. Overall equilibrium water solubility of the non-aqueous phase liquid (NAPL) present in the sample and the water phase's chemical composition (in terms of the 79 fractions defined) are then calculated using Raoult's law. The calculation method was validated using soil spiked with 13 different TPH mixtures and 1 field-contaminated soil. Measured water solubilities using a column recirculation equilibration experiment agreed well to calculated equilibrium concentrations and water phase TPH composition.     

Liquid–Liquid Equilibria of the Methanol + Toluene + Methylcyclohexane Ternary System at 278.15, 283.15, 288.15, 293.15, 298.15 and 303.15 K

Liquid–liquid equilibria of the methanol + toluene + methylcyclohexane ternary system at 278.15, 283.15, 288.15, 293.15, 298.15 and 303.15 K are reported. The effect of the temperature on liquid–liquid equilibrium is discussed. Data for the ternary system is available from the literature at T = 298 K. All chemicals were quantified by gas chromatography using a thermal conductivity detector. Experimental data for the ternary system are compared with values calculated by the NRTL and UNIQUAC equations. It is found that the UNIQUAC and NRTL models provide similar good correlations of the solubility curve at these six temperatures.     

Calorimetric investigation of the RbFRb2SO4 liquid system and comparison of the excess thermodynamic functions in the AFA2SO4 (ALi,Na, K,Rb) molten salt mixtures

The experimental values of the excess enthalpy, obtained by direct calorimetry, are reported in this work for the RbFRb₂SO₄ liquid system. The entropy of mixing of this system was calculated from the equilibrium phase diagram.Many expressions have been presented in the literature for the ideal entropy of mixing of ABin2A′B asymmetrical systems and we have pointed out, here, a criterion allowing the selection of one of them for a further evaluation of the excess entropy.A comparative study of the thermodynamic excess functions (δH,δS^E)was carried out on the series of AFA₂SO₄ mixtures (ALi, Na, K, Rb).     

Formation and decomposition of gas hydrates of natural gas components

Based on our theoretical and experimental work carried out during the last decade, our understanding of the thermodynamics and the kinetics of formation and decomposition of gas hydrates is presented. Hydrate formation is modelled as a crystallization process where two distinct processes (nucleation and growth) are involved. Prior to the nucleation the concentration of the gas in the liquid water exceeds that corresponding to the vapor-liquid equilibrium. This supersaturation is attributed to the extensive structural orientation in the liquid water and is necessary for the phase change to occur. The growth of the hydrate nuclei or the decomposition of a hydrate particle are modelled as two-step procedures. Only one adjustable parameter for each hydrate forming gas is required for the intrinsic rate of formation or decomposition. In addition the inhibiting effects of electrolytes or methanol on hydrate formation are discussed and experimental data on methane gas hydrate formation in the presence of aqueous solutions of 3% NaCl and 3% NaCl + 3% KCI, are presented along with the predicted values. Finally, the relevence of the ideas to the technological implications of gas hydrates as well as areas where future research is needed are discussed.Dedicated to Dr D. W. Davidson in honor of his great contributions to the sciences of inclusion phenomena.     

Liquid—liquid equilibrium in methanol + gasoline blends

An investigation has been carried out to study the limited miscibility of methanol and gasoline blends over the temperature range −20 to 20°C. Two liquid phases in equilibrium were analysed by mass spectrometric methods and their composition reported, in addition to the methanol content, in terms of six principal classes of hydrocarbons. Liquid—liquid equilibrium was predicted using the UNIFAC group contribution model. In liquidliquid equilibrium calculations, gasoline was represented by a set of model compounds. The number of the different groups that comprise each model molecule was determined using the result of a distillation analysis and the paraffin—naphthene—aromatic composition. Estimation of conjugate phase composition using the UNIFAC model is reasonable at temperatures above 0°C. To describe correctly the limited miscibility of methanol+gasoline blends over the whole temperature range studied, we found that ‘specific’ UNIFAC interaction parameters were necessary.     

Phase equilibrium study of the binary systems (N-hexyl-3-methylpyridinium tosylate ionic liquid + water,or organic solvent)

The (solid + liquid) phase equilibrium (SLE) and (liquid + liquid) phase equilibrium (LLE) for the binary systems ionic liquid (IL) N-hexyl-3-methylpyridinium tosylate (p-toluenesulfonate), {([HM³Py][TOS] + water, or an alcohol (1-butanol, or 1-hexanol, or 1-octanol, or 1-decanol), or an aromatic hydrocarbon (benzene, toluene, or ethylbenzene, or propylbenzene), or an alkane (n-hexane, n-heptane, n-octane)} have been determined at ambient pressure using a dynamic method. Simple eutectic systems with complete miscibility in the liquid phase were observed for the systems involving water and alcohols. The phase equilibrium diagrams of IL and aromatic or aliphatic hydrocarbons exhibit eutectic systems with immiscibility in the liquid phase with an upper critical solution temperature as for most of the ILs. The correlation of the experimental data has been carried out using the UNIQUAC, Wilson and the non-random two liquid (NRTL) correlation equations. The results reported here have been compared with analogous phase diagrams reported by our group previously for systems containing the tosylate-based ILs.     

On the influence of some inorganic salts on the partitioning of citric acid between water and organic solutions of tri-n-octylamine: Part I: Methyl isobutyl ketone as organic solvent

Reactive extraction is a commonly applied process to recover carboxylic acids from aqueous solutions. Such processes are nowadays designed using process simulation software. However, the essential prerequisite for such a simulation is the availability of a reliable thermodynamic model for the encountered phase equilibrium. Industrial experience revealed that even very small amounts of a strong electrolyte (e.g., sodium chloride) can considerably reduce the amount of carboxylic acid extracted from the aqueous into the organic phase. This contribution presents new experimental results for the influence of sodium nitrate, sodium chloride, sodium sulfate, sodium citrate and hydrochloric acid on the partitioning of citric acid to the coexisting aqueous/organic liquid phases of the system water + methyl isobutyl ketone (organic solvent) + tri-n-octylamine (chemical extractant) at 25 °C. A detailed discussion of the experimental results reveals that the dramatic decrease of the partition coefficient of carboxylic acid is caused by the chemical loading of the extractant by the inorganic acid, i.e. both acids (the weak carboxylic acid as well as the strong inorganic acid) compete for the sodium ions (in the aqueous phase) and for the amine (in the organic phase). In phase equilibrium the amine is predominantly loaded with the inorganic acid while the sodium salt of the carboxylic acid remains in the aqueous phase. That behavior is described by a thermodynamic framework that is able to predict the complex liquid–liquid equilibrium from information determined exclusively from investigations on subsystems.