Bubble temperature measurements on the binary mixtures formed by decane with a variety of compounds at 95.8 kPa
Introduction
This investigation leading to the vapor–liquid equilibria of the binary mixtures formed by decane with the variety of compounds (noted in the abstract) is in continuation of our recent systematic studies on the phase equilibria of the binary mixtures formed by alcohols, hydrocarbons and chlorohydrocarbons [1], [2]. There are no published vapor–liquid equilibrium data on the systems chosen for the present study for comparison.
Section snippets
Method
A Swietoslawski type ebulliometer, very similar to the one described by Hala et al. [3] is used for the present set of experiments. The ebulliometer is connected to a vacuum pump and a dry nitrogen gas cylinder, with a closed end manometer in line, to enable the measurement and maintenance of the total pressure of the system within ±0.1 kPa of the chosen value 95.8 kPa, by adjusting the opening of: the needle valve of the gas cylinder or the by pass line of the vacuum pump. A mercury-in-glass
Results and discussion
The experimental composition (x1) versus temperature (T) data, summarized in Table 2 (which also includes estimated values of the vapor phase composition, y1) is fitted to the Wilson model.withandwhere λ's are the energies of interaction denoted by the subscripts. The optimum Wilson parameters are obtained by minimizing
References (6)
- et al.
J. Chem. Eng. Data
(2001) - et al.
Fluid Phase Equilib.
(2002) - et al.
Vapour Liquid Equilibrium
(1958)
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