Reactive extraction of valeric acid from water by tri-n-propyl amine (TPA) and dibenzyl amine (DBA) dissolved in polar oxygenated aliphatic diluents (diethyl sebacate, diethyl succinate, diethyl malonate, ethyl caprylate, ethyl valerate and isoamyl alcohol) has been studied at 298 0.2 K T = ± and P 101.3 0.7 kPa p = ± . Distribution data have been subjected to formulation of an optimization structure for effective acid separation. The optimization approach uses separation ratio R and synergistic enhancement SE factors to efficiently identify optimum extraction ranges. Among the examined alipha tic ester and alcohol diluents, monoesters exhibit higher solvation efficiency comprising acid 1 -amine 1 complex formation, while isoamyl alcohol yields larger loading factors. The uptake capacity of the amine/diluent system is ranging in the order TPA > DBA.Modeling efforts based on the mass-action law principles have shown considerable success. The mass action law chemodel and modified Langmuir approach are quite accurate yielding mean errors of 0.9 % and 0.7 %, respectively.
This paper studies liquid‐liquid equilibrium (LLE) of the type 2 systems (water + valeric acid + dibasic ester or monobasic ester or alcohol) at T = (298.2 ± 0.1) K and p = (101.3 ± 0.7) kPa. Equilibrium distribution of valeric acid onto (water + solvent) two‐phase system is better for more structured diethyl sebacate and ethyl caprylate as compared to less structured diethyl succinate, diethyl malonate, ethyl valerate, and isoamyl alcohol. The two‐phase envelope size and the tie line slope on the phase diagrams are varying as follows: ethyl caprylate > diethyl sebacate > ethyl valerate > diethyl succinate ≈ diethyl malonate > isoamyl alcohol. The SERLAS‐integrated (solvation energy relation for liquid associated systems‐integrated) molecular model with nine physical descriptors, originated from LSER (linear solvation energy relation) principles in conjunction with group‐contribution method, is proposed and applied to the prediction of type 2 LLE properties. By combining SERLAS with UNIFAC‐Dortmund, we are able to get along with a simultaneous impact of both methods for satisfactorily simulating type 2 phase behaviour so long as solvent effects are concerned. SERLAS, SERLAS‐modified, SERLAS‐integrated, and UNIFAC‐original models have been stringently tested for consistency in reproducing phase equilibrium properties with average deviations inferior to 28.8 %, 44.3 %, 21.3 %, and 30.4 %, respectively.
Liquid-liquid equilibrium data of water + formic acid + acetic acid + solvent (amyl acetate, diisobutyl ketone, and diisopropyl ether) quaternary systems were measured at 298.15 K and atmospheric pressure. Complete phase diagrams were obtained by determining solubility curves and tie-lines. A comparison of the extracting capabilities of the solvents was made with respect to distribution coefficients, separation factors, and solvent-free selectivity bases. Reliability of the data was ascertained from Othmer-Tobias plots. The tie-lines were also predicted using the UNIFAC model. It is concluded that the used solvents can be treated as suitable separating agents for dilute aqueous formic and acetic acid mixtures.
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