Liquid–Liquid Equilibrium Data for the Ternary Systems of Water, Isopropyl Alcohol, and Selected Entrainers

Abstract

In this study, a substitutive entrainer is found for the azeotropic process of water and isopropyl alcohol (IPA). Liquid−liquid equilibrium (LLE) data are measured for the ternary systems of water−IPA−benzene, water−IPA−cyclohexane, and water− IPA−hexane at three different temperature values: 303, 313, and 323 K. The liquid−liquid equilibrium data are developed via an experimental setup equipped with equilibrium cell, magnetic stirrer, and gas chromatography units. Equilibrium compositions for the water−IPA system are found by using three different entrainers: benzene, cyclohexane, and hexane. Parameters calculated by nonrandom two-liquid (NRTL) and universal quasichemical (UNIQUAC) thermodynamic models are compared with the data obtained by experiments, and the comparison shows a good correlation between thermodynamic models and the experimental data.

Influence of Temperature on the Liquid–Liquid Phase Equilibria of Ternary (Water + Alcohol + Entrainer) Systems

“…Considering the (water + propanol + hydrocarbon) systems, Plačkov and Štern , report failed NRTL and UNIQUAC correlations for the LLE of (water + isopropanol/ n -propanol + cyclohexane) systems at 298.2 K, whereas Battler et al report failed NRTL and UNIQUAC correlations for the LLE of (water + isopropanol + cyclohexane) over the temperature range 293.2 to 303.2 K. Choi et al also report very large AADs (in the order of 0.2 mole fraction) for their correlation of the (water + isopropanol + cyclohexane) system with the UNIQUAC model. Lee and Shen further report a failed UNIQUAC correlation for the VLLE of the (water + n -propanol + cyclohexane) system.…”

Explorations of Liquid–Liquid Phase Equilibrium for the Mixture (Isopropanol + Water) with Pyridinium-Based Ionic Liquids

“…Generally, IPA is mainly produced by the propylene hydration method in industry, from which an aqueous mixture of IPA is obtained. Because IPA and water can generate a minimum azeotrope with 87.8 wt % IPA at the azeotropic temperature of 353.45 K under 101.3 kPa, , general distillation is unavailable to purify IPA. Usually, for the purpose of separating such mixtures, extractive distillation, , pressure swing distillation, and azeotropic distillation are applied in industry.…”

Liquid–Liquid Equilibrium Data of Water + Butyric Acid + {Butanal or n-Butanol} Ternary Systems at 293.15, 308.15, and 323.15 K

“…Extraction is generally considered as a feasible way of separating butyric acid from aqueous solutions due to its less energy consumption . Liquid–liquid equilibrium (LLE) data are useful in extraction processes because they can provide effective information for the optimization or excogitation of separation. − During the past time, heavy alcohols or alkanes were adopted as extraction agents in the separation of butyric acid from aqueous solutions, and the LLE data were measured and reported in literature. − However, considering the fact that there is usually a certain amount of n -butanol and butanal in the oxidized mixture, the extraction process of butyric acid from aqueous solutions includes the multicomponent liquid–liquid equilibrium (water, butyric acid, butanal, n -butanol, and so on). Moreover, the ternary LLE data can be used as the necessary basic data in investigating multicomponent liquid–liquid equilibrium, and there are generally two possible ternary systems (water + butyric acid + butanal, water + butyric acid + n -butanol) in the extraction process of butyric acid from the oxidized mixture.…”