Isothermal (vapor + liquid) equilibrium data are reported for the binary mixtures containing (nitromethane or nitroethane) + 1,4-dichlorobutane) at three temperatures, (343.15, 353.15, 363.15) K. The measurements were performed by means of an ebulliometer which allows sampling from both phases in equilibrium. The experimental data were correlated using the Redlich-Kister, Wilson, NRTL and UNIQUAC excess Gibbs energy models by means of maximum likelihood

Isothermal vapor
liquid equilibrium (VLE) data are reported at three temperatures, (343.15, 353.15, and 363.15) K, for the binary mixtures containing nitromethane or nitroethane with 1,3-dichloropropane. For the measurements an all-glass ebulliometer was used, which allows sampling from both phases in equilibrium. The experimental data were correlated using the nonrandom two-liquid (NRTL) and universal quasichemical activity coefficient (UNIQUAC)

The vapour pressures of binary mixtures of methyl ethyl ketone (2-butanone) + chloroalkanes (1-chloropentane, + 1,1,1-trichloroethane, + 1,1,2,2-tetrachloroethane) were measured by a static total pressure method, at temperatures between 298.15 K and 318.15 K. The vapour pressures vs. liquid phase composition data have been used to calculate the activity coefficients of the two components, and the excess molar Gibbs energies GE for the mixtures, using

The vapour pressures of binary mixtures of cyclohexanone + dichloroalkane (1,3-dichloropropane and 1,4-dichlorobutane) were measured at temperatures between 298.15 and 318.15 K. The vapour pressures vs. liquid phase composition data were used to calculate the activity coefficients of the two components and the excess molar Gibbs energies GE for the mixtures, using the Barker method and the Redlich–Kister, Wilson, NRTL and UNIQUAC equations, taking

Isothermal vapour–liquid equilibrium (VLE) data are reported at three temperatures, 333.15, 343.15 and 353.15 K, for binary mixtures containing 1,2-dichloroethane with nitromethane or nitroethane. Use has been made of an ebulliometer which allows sampling from both phases in equilibrium. The experimental data were correlated using the Redlich–Kister, Wilson, NRTL and UNIQUAC excess Gibbs energy models by means of the maximum likelihood method,

The experimental densities of binary mixtures of cyclopentanone with 1,1,2,2-tetrachloroethane, 1,1,1-trichloroethane, trichloromethane, 1,2-dichloroethane, 1,3-dichloropropane, 1,4-dichlorobutane, and 1-chlorobutane have been measured at T = (288.15, 298.15, 308.15, and 318.15) K and atmospheric pressure, over the whole composition range. From these results, excess molar volumes, VE, have been calculated and fitted to the Redlich−Kister polynomial

Excess molar volumes (VE) have been measured for binary liquid mixtures of cyclohexanone or cyclopentanone with 1,1,2,2-tetrachloroethane, 1,1,1-trichloroethane, trichloromethane, 1,2-dichloroethane, 1,3-dichloropropane, 1,4-dichlorobutane and 1-chlorobutane at T = (288.15, 298.15, 308.15, and 318.15) K and atmospheric pressure. The VE data were analysed with the Flory and Prigogine-Flory-Patterson (PFP) statistical theories of solutions. The obtained

The experimental densities of binary mixtures of cyclohexanone with 1,1,2,2-tetrachloroethane, 1,1,1-trichloroethane, trichloromethane, 1,2-dichloroethane, 1,3-dichloropropane, 1,4-dichlorobutane and 1-chlorobutane have been measured at T = (288.15, 298.15, 308.15, and 318.15) K and atmospheric pressure, over the whole composition range. From these results, excess molar volumes, VE, have been calculated and fitted to Redlich–Kister polynomial equation.

The vapour pressures of binary (cyclohexanone + 1-chlorobutane, + 1,1,1-trichloroethane) mixtures were measured at the temperatures of(298.15, 308.15, and 318.15) K. The vapour pressures vs. liquid phase composition data have been used to calculate the excess molar Gibbs free energies GE of the investigated systems, using Barker’s method. Redlich–Kister, Wilson, UNIQUAC, and NRTL equations, taking into account the vapour phase imperfection in