Isothermal vapour–liquid equilibria in the binary and ternary systems composed of 2-propanol, diisopropyl ether and 1-methoxy-2-propanol
Introduction
The data of a continuing project dealing with phase equilibria in mixtures belonging to distinct families of organic compounds are reported in this paper. Vapour–liquid equilibria are determined for two binary and one ternary systems containing alcohol, ether, and alkoxyalcohol. Within the series of papers, the system of components having common alkyl group (isopropyl), namely, 2-propanol + diisopropyl ether + 2,2,4-trimethylpentane has already been investigated [1]. Analogously, the tert-butyl methyl ether + tert-butanol + 2,2,4-trimethylpentane or with 1-tert-butoxy-2-propanol systems containing components with common tert-butyl group in their structure were investigated in the previous papers [2], [3]. Compounds used throughout this paper consist also of both the ether and alcohol and isopropyl groups: 2-propanol, diisopropyl ether, and 1-methoxy-2-propanol. The new data were measured at the two constant temperature levels particularly at 330.00 and 340.00 K, in order to be consistent with the first paper [1].
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Apparatus and procedure
Experimental vapour–liquid equilibrium data were measured in an all glass circulation still chargeable with 150 ml of liquid phase; essentially it was the Dvorak–Boublik type with modifications described in detail elsewhere [4]. The pressure was measured indirectly via the boiling point of water in an ebulliometer connected in parallel to the still; the relative accuracy is ±0.1% of measured value. The equilibrium temperature was determined with the digital thermometer S1220 (Systemteknik,
Results
At first, vapour pressures of pure 1-methoxy-2-propanol were measured in the same experimental set-up. The experimental data are summarized in Table 1; they were correlated by the Antoine equation with use of the maximum likelihood method. The standard deviations necessary for calculation were estimated as 0.01 K for temperature and 0.05% of measured value for pressure. The resulting equation with evaluated parameters is . The deviations between
Discussion and conclusions
No published vapour–liquid equilibrium data for the systems under study were found in the bibliography covering the period 1888–2002 [11]; not even vapour pressures for 1-methoxy-2-propanol have been measured earlier. Therefore, no comparison with literature data was possible. However, the reliability of both the data and correlation procedure is verified by the fact that the resulting standard deviations are approximately proportional to the magnitudes of uncertainties input. Generally, the
Acknowledgements
The authors would like to acknowledge the partial support of the Grant Agency of the Czech Republic; the work has been carried out under Grant No. 104/03/1555.
References (12)
- et al.
Fluid Phase Equilib.
(2001) - et al.
Fluid Phase Equilib.
(2001) - et al.
Fluid Phase Equilib.
(1998) - I. Wichterle, ELDATA: Int. Electron. J. Phys. Chem. Data 5 (1995)...
- J. Timmermans, Physico-Chemical Constants of Pure Organic Compounds, vols. 1 and 2, Elsevier, Amsterdam, 1950,...
- J.A. Riddick, W.B. Bunger, Organic solvents: in: Techniques of Chemistry, vol. 2, Wiley–Interscience, New York,...
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