Elsevier

Fluid Phase Equilibria

Volume 382, 25 November 2014, Pages 286-299
Fluid Phase Equilibria

Experimental isobaric vapor–liquid equilibrium at atmospheric and sub-atmospheric pressures, excess molar volumes and deviations in molar refractivity from 293.15 K to 318.15 K of diisopropyl ether with methanol and isopropyl alcohol

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Abstract

Experimental isobaric vapor–liquid equilibrium data for the binary systems, diisopropyl ether + isopropyl alcohol and methanol + diisopropyl ether at the local atmospheric pressure of 94.79 kPa and at sub-atmospheric pressures of (53.3, 66.7, 79.9) kPa were obtained over the entire composition range using a Sweitoslawsky-type ebulliometer. The experimental temperatures were compared with predictions made using Wilson, NRTL, UNIQUAC, UNIFAC, Peng–Robinson (PR) and Soave–Redlich–Kwong (SRK) equations of state (EoS) with Wong–Sandler (WS) mixing rules. Model parameters along with the deviations in temperature have been presented. Experimental temperatures were found to be in good agreement with the predicted values. NRTL model was found to represent the VLE behavior of these systems better than the other models used. Density and refractive indices of mixtures are reported from 293.15 K to 318.5 K.

Introduction

The binary systems studied experimentally in this work, diisopropyl ether (DIPE) + isopropyl alcohol (IPA) and methanol + DIPE are part of the study of the vapor–liquid equilibrium (VLE) behavior of the ternary system, methanol + DIPE + IPA. DIPE is a potential eco-friendly gasoline additive [1] and an important solvent in the industry. It is found in the downstream of various industries such as in acetone manufacturing [2] and it can be synthesized from isopropanol. In the present study we have experimentally investigated the isobaric vapor–liquid equilibrium behavior of these binary systems at the local atmospheric pressure and sub-atmospheric pressures. Densities and refractive indices of the mixtures at various compositions have been measured from 293.15 K to 318.5 K. The work reported here is in continuation with our previous studies of phase equilibria and properties of industrially important streams containing alcohols, hydrocarbons and halogenated organics [3], [4], [5]. Chamorro et al. [1] have reported an azeotrope for the DIPE + IPA binary system as part of the isothermal VLE data of the binary and ternary systems containing DIPE, IPA and n-heptane at 313.15 K and Lladosa et al. [6] have studied this system at 30 and 101.3 kPa. Frakova et al. [7] have reported isothermal VLE data for the methanol + DIPE system at 320 and 330 K.

Section snippets

Materials Used

Methanol (>99.8 mass %, HPLC grade) provided by SD Fine Chemicals, India and diisopropyl ether (>98.5 mass %, GC grade) and isopropyl alcohol (>99.8 mass %, HPLC grade) supplied by Sigma–Aldrich were used for experimentation. The chemicals were stored in dessicators to prevent absorption of moisture and were used without any further purification. The final purity of the compounds was measured by a ZB-5 column using FID detector on a Shimadzu 2010 gas chromatograph. The densities and refractive

Pure component vapor pressures

Vapor pressures of the pure components IPA and methanol were measured in the same experimental set-up used for the VLE studies. The P–T data are given in Table 2, Table 3. The experimental pure component vapor pressures were found to be in good agreement with values obtained using Antoine constants given by Reid et al. [14] in Eq. (1).lnPi0(torr)=AiBiT(K)+CiThe deviation in the vapor pressures, ΔPi0=ΔPi,lit0ΔPi,exp0 is represented graphically in Fig. 1, Fig. 2 for IPA and methanol

Conclusions

The experimental T−x1 data for DIPE + IPA and methanol + DIPE systems were measured at atmospheric and sub-atmospheric pressures using a modified Sweitoslawsky ebulliometer. Activity coefficient models, Wilson, NRTL, UNIQUAC, group contribution method UNIFAC and EoS models PR, SRK with WS mixing rules have been fitted to the experimental data and the optimized model parameters have been reported. Temperature predictions of all the models except UNIFAC are in good agreement with the experimental

References (21)

  • J.M. Resa et al.

    Fluid Phase Equilib.

    (1999)
  • J. Soujanya et al.

    J. Chem.Themodyn.

    (2010)
  • P. Gnanakumari et al.

    Fluid Phase Equilib.

    (2007)
  • T.E. Vittal Prasad et al.

    Fluid Phase Equilib.

    (2002)
  • E. Lladosa et al.

    Fluid Phase Equilib.

    (2007)
  • J. Farkova et al.

    Fluid Phase Equilib.

    (1995)
  • J.M. Resa et al.

    Fluid Phase Equilib.

    (2001)
  • J. Pavlicek et al.

    Fluid Phase Equilib.

    (2013)
  • L. Xiao et al.

    Fluid Phase Equilib.

    (2013)
  • H.Y. Kwak et al.

    Fluid Phase Equilib.

    (2007)
There are more references available in the full text version of this article.

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