Representation of VLE and liquid phase composition with an electrolyte model: application to H3PO4–H2O and H2SO4–H2O

2002 ◽  
Vol 194-197 ◽  
pp. 729-738 ◽  
Author(s):  
Mourad Cherif ◽  
Arbi Mgaidi ◽  
Mohamed Naceur Ammar ◽  
Manef Abderrabba ◽  
Walter Fürst
Keyword(s):  
Phase Composition ◽  
Liquid Phase ◽  
Model Application ◽  
Liquid Phase Composition

Modelling of the equilibrium properties of the system H3PO4–H2O: representation of VLE and liquid phase composition

2000 ◽  
Vol 175 (1-2) ◽  
pp. 197-212 ◽  
Author(s):  
Mourad Cherif ◽  
Arbi Mgaidi ◽  
Mohamed Naceur Ammar ◽  
Manef Abderrabba ◽  
Walter Fürst
Keyword(s):  
Phase Composition ◽  
Liquid Phase ◽  
Liquid Phase Composition

Soil Liquid Phase Composition

Soil Science ◽  
2003 ◽  
Vol 168 (5) ◽  
pp. 383
Author(s):  
Dennis E. Rolston
Keyword(s):  
Phase Composition ◽  
Liquid Phase ◽  
Liquid Phase Composition

Equilibrium Modeling of Lead Adsorption onto a “Red Soil” as a Function of the Liquid-Phase Composition

2002 ◽  
Vol 41 (8) ◽  
pp. 1946-1954 ◽  
Author(s):  
Marco Petrangeli Papini ◽  
Annalisa Bianchi ◽  
Mauro Majone ◽  
Mario Beccari
Keyword(s):  
Phase Composition ◽  
Liquid Phase ◽  
Red Soil ◽  
Lead Adsorption ◽  
Equilibrium Modeling ◽  
Liquid Phase Composition

scholarly journals Isothermal vapour-liquid equilibria in cyclohexanone + dichloroalkane binary mixtures at temperatures from 298.15 to 318.15K

2011 ◽  
Vol 76 (2) ◽  
pp. 305-315 ◽  
Author(s):  
Dana Dragoescu ◽  
Alexandru Barhala ◽  
Mariana Teodorescu ◽  
Daniela Chiscan
Keyword(s):  
Phase Composition ◽  
Liquid Phase ◽  
Binary Mixtures ◽  
Activity Coefficients ◽  
Virial Coefficient ◽  
Vapour Phase ◽  
Composition Data ◽  
Gibbs Energies ◽  
Significant Difference ◽  
Liquid Phase Composition

The vapour pressures of binary mixtures of cyclohexanone + dichloroalkane (1,3-dichloropropane and 1,4-dichlorobutane) were measured at temperatures between 298.15 K 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 into account the vapour phase imperfection in terms of the 2nd virial coefficient. No significant difference between the GE values obtained with these equations was observed.

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