Aleksandar Z. Tasic

Excess volumes of acetone + benzene, acetone + cyclohexane, and acetone + benzene + cyclohexane at 298.15 K☆

Abstract Excess volumes of the binaries: acetone + benzene and acetone + cyclohexane, and for the ternary: acetone + benzene + cyclohexane, have been determined from density measurements at 298.15 K. Analytical expressions which represent the composition dependences of the excess volumes are reported.

Vapour—liquid equilibria of the systems acetone—benzene, benzene—cyclohexane and acetone—cyclohexane at 25°C

Vapour—liquid equilibrium data for the binary systems acetone—benzene, benzene—cyclohexane and acetone—cyclohexane have been determined experimentally at 25°C. The reduction producers based on P - x - y as well as on P - x isothermal data sets, which incorporate usual thermodynamically consistent models expressing the dependence of activity coefficients of liquid composition, have been examined for representing the reported results. Nonideal behaviour of the both phases has been taken into account. Thermodynamic consistency of the data has been shown by comparing of the experimentally obtained vapour compositions with those calculated from P - x data using the best of the examined models for activity coefficients.

Mixing cell for indirect measurements of excess volume

Abstract A mixing cell suitable for making liquid mixtures of accurately known composition is described and has been tested by measurements of the excess volume of benzene + cyclohexane.

Thermodynamic Modeling of Vapor-Liquid Equilibria and Excess Properties of the Binary Systems Containing Diethers and n-Alkanes by Cubic Equation of State

A comparison of the performances of two different approaches of cubic equations of state models, based on a classical van der Waals and mixing rules incorporating theGE equation, was carried out for correlation of Vapor-Liquid Equilibria (VLE), HE and CPE data alone, and simultaneous correlation of VLE+HE, VLE+CPE, HE +CPE and VLE+HE +CPE data for the diethers (1,4-dioxane or 1,3-dioxolane) with n-alkane systems. For all calculations the Peng-Robinson-Stryjek-Vera cubic equation of state (PRSV CEOS) was used. A family of mixing rules for the PRSV CEOS based on the Modified van der Waals one-fluid mixing rule (MvdW1) and two well-known CEOS/GE mixing rules (MHV1 and MHV2), was considered. The NRTL equation, as the GE model with linear or reciprocal temperature dependent parameters, was incorporated in the CEOS/GE models. The results obtained by the CEOS/GE models exhibit significant improvement in comparison to the MvdW1 models.

Phase equilibrium calculations for ethylene-multicomponent polyethylene mixtures at high pressures

Abstract In this work, the phase equilibrium data for ethylene—multicomponent polyethylene have been predicted using the free volume theory of polymer solutions. The calculations have been performed for the conditions which are normally maintained in the reactor during production of “two phase” polyethylene resins. The results obtained can be used for a kinetic explanation of ethylene polymerization under heterogeneous conditions and for the study of the influence of the amount of polymer formed under two phase conditions on the final properties of commercial low-density polyethylene.