(Liquid + liquid) equilibria in ternary aqueous mixtures of phosphoric acid with organic solvents at T = 298.2 K
Introduction
Studies of phase equilibria of ternary systems are very important in both theoretical and industrial applications. Precise LLE data of aqueous mixtures with organic solvents are needed in the evaluation of industrial units for solvent extraction processes. The accurate interpretation of phase equilibria and thermodynamic behaviour for the different ternary mixtures is a fundamental and important key to improving solvent extraction techniques [1], [2], [3], [4], [5], [6], [7], [8], [9].
Phosphoric acid is one of the most widely used inorganic acids, which has many industrial applications. The pure phosphoric acid is extensively used as an additive in the food industry. Therefore, the efficient separation of phosphoric acid from aqueous solutions, by solvent extraction technique, is of considerable economic importance in the chemical industry [10], [11], [12].
The type of solvent is one of the most important factors, which influence the equilibrium characteristics of extraction of the acid from aqueous solutions. Many organic solvents have been tested as extractants for the recovery and purification of phosphoric acid from water. Heavy alcohols, ketones and ethers have mainly been used for extraction of phosphoric acid from aqueous solutions [13], [14], [15], [16], [17], [18], [19], [20].
From practical and economical aspects, the search for new and suitable organic solvents for the separation of phosphoric acid from water is a current study. We have recently reported [21] LLE results for the aqueous mixtures of phosphoric acid with 1-butanol and butyl acetate at T = 308.2 K, where a Type 1 (liquid + liquid) phase diagram was obtained for both the ternary systems. As a continuation of that previous work, we present the LLE results for the three ternary systems (water + phosphoric acid + cyclohexane), (water + phosphoric acid + isobutyl acetate), (water + phosphoric acid + 2-methyl-2-butanol) at T = 298.2 K. These organic solvents widely used as extractants to determination of LLE data for many ternary mixtures [22], [23], [24], [25], [26], [27], [28], [29].
In order to evaluate the extracting capability of the solvents for the separation of the acid from aqueous solutions with (liquid + liquid) extraction, the separation factor (S) was calculated. The experimental LLE values were correlated using the non-random two-liquid (NRTL) model of Renon and Prausnitz [30] and the interaction parameters were obtained. The LLE values were then analyzed in terms of root mean square deviations (RMSD) between experimental and calculated compositions in both equilibrium phases.
Section snippets
Materials
Cyclohexane and 2-methyl-2-butanol with stated mass fraction purity higher than 0.99 were obtained from Merck. The isobutyl acetate, with stated mass fraction purity higher than 0.98, was supplied by Merck. For the study of the equilibrium data, analytical grade phosphoric acid containing 85 wt% (Merck) was used. The purity of the acid was checked through acidimetric titration with 1 N NaOH. Deionised and redistilled water was used throughout all the experiments. All materials were used as
Experimental LLE results
The experimental tie-line data for the ternary systems {water + phosphoric acid + organic solvents (cyclohexane, isobutyl acetate, and 2-methyl-2-butanol)} were determined at T = 298.2 K. The experimental and the correlated values for each ternary system are listed in table 1. The LLE phase diagrams for these ternary systems are plotted and are shown in FIGURE 1, FIGURE 2, FIGURE 3.
Since the (water + organic solvent) mixture is the only pair that is partially miscible and two liquid pairs (phosphoric
Conclusion
Tie-line data for the {water (1) + phosphoric acid (2) + cyclohexane (3)}, {water (1) + phosphoric acid (2) + isobutyl acetate (3)}, and {water (1) + phosphoric acid (2) + 2-methyl-2-butanol (3)} ternary systems were obtained at T = 298.2 K. Each ternary system exhibits Type-1 behaviour of the LLE. The NRTL (α = 0.3) model was used to correlate the experimental LLE results and to calculate the phase compositions of the studied mixtures. The corresponding optimized binary interaction parameters were also
References (34)
- et al.
Fluid Phase Equilib.
(1995) - et al.
Fluid Phase Equilib.
(1999) Fluid Phase Equilib.
(2006)- et al.
Fluid Phase Equilib.
(1996) - et al.
Fluid Phase Equilib.
(2001) Fluid Phase Equilib.
(2005)J. Chem. Thermodyn.
(2007)- et al.
Fluid Phase Equilib.
(2008) Solvent Extr. Rev.
(1971)- et al.
Fluid Phase Equilib.
(1998)