A good understanding and prediction of the phase equilibrium of the fatty acid methyl ester (FAME) + glycerol + methanol ternary system is needed to design and optimize the separation unit of the biodiesel production process. In this work, new experimental vapor−liquid−liquid data on the ternary system have been measured at temperatures between 333.15 and 473.15 K. In addition, new data have been gathered on the methanol + glycerol [vapor−liquid equilibrium (VLE)] and methanol + methyl oleate (VLE and liquid−liquid equilibrium) binary systems. A group contribution method combined with a statistical associating fluid theory equation of state (GC-PPC-SAFT) proposed earlier by our group (Group contribution method with SAFT EOS applied to vapor liquid equilibria of various hydrocarbons series Tamouza S. Passarello J.-P. Tobaly P. de Hemptinne J.-C. Tamouza S. Passarello J.-P. Tobaly P. de Hemptinne J.-C. Fluid Phase Equilib.20042222236776) and recently extended to predict VLE of heavy esters and their mixtures (Predicting VLE of heavy esters and their mixtures using GC-SAFT Nguyen Huynh D. Falaix A. Passarello J.-P. Tobaly P. de Hemptinne J.-C. Nguyen Huynh D. Falaix A. Passarello J.-P. Tobaly P. de Hemptinne J.-C. Fluid Phase Equilib.2008264184200) is here applied to model vapor liquid−liquid equilibria of methanol + glycerol + methyl oleate. The SAFT parameters for the glycerol pure component have been regressed using two association schemes (4C and 3X2B). The dispersive binary interaction parameters kij have been regressed on the binary systems. The group contribution scheme was used for predicting the ester properties.

New isobaric vapor−liquid equilibria data were measured for N,N-dimethyl-1-butanamine + n-hexane, n-heptane, 1-propanol, 1-butanol, or 1-pentanol and N,N-dimethyl-1-octanamine + n-heptane or 1-butanol binary mixtures. The boiling temperatures of both pure amines were also investigated. For this, an ebulliometer based on Cottrell's apparatus was used. Thus, 180 new mixture data points displayed on 35 isobars were obtained in a pressure range from (29.84 to 99.83) kPa and in the full composition range. The experiments were compared with the Group contribution polar perturbed chain statistical associating fluid theory (GC-PPC-SAFT) equation of state predictions for pure amines and the mixtures containing an alkane. In the case of the systems containing an alkanol, the binary interaction parameters needed to be fitted.

A new experimental apparatus has been developed to measure vapor− liquid equilibria (VLE) and vapor−liquid−liquid equilibria (VLLE) for multicomponent systems containing light hydrocarbons, carbon dioxide, methanol, and water at low temperatures. These systems are particularly difficult to investigate experimentally because of the polarity contrast existing between the polar and nonpolar components. In such systems, the phase equilibrium leads to a heterogeneous distribution of the different components into the different phases. Nevertheless, such systems are frequently met in refining processes and in gas treatment. Consequently, it is very important to investigate them experimentally in order to improve the engineering processes. In the present study, we describe a new apparatus which allows to investigate fluid phase equilibrium at low temperature. The experimental setup is presented in detail and the experimental procedures to reach and measure vapor−liquid and vapor−liquid−liquid equilibrium are explained. This equipment has been tested on the methanol−ethane binary system.

The usual method for determining the gas in place (GIP) in a reservoir uses a balance equation based on laboratory measurements of the raw gas volumetric factor as a function of pressure on a waterfree basis. In the reservoir, however, the gas is saturated with water. Volumetric measurements at high temperatures and pressures have been performed on a North Sea fluid at 374°F, both in water-free conditions and in the presence of an excess water. The water content of the gas at 650 bar has been determined to be 3.5 mol% (3.6 mole of water/100 mole of reservoir fluid) water-saturated reservoir fluid. A corresponding volume increase of 3.2 % has been detected. These experimental measurements have been correlated with a Tait-type equation. The Søreide and Whitson 1 model has been used to calculate the water content of the gas. A modified balance equation is proposed for prediction of the GIP. MoracchiniBrunella de Hemptinne Zhou

Résumé -Solutibilités mutuelles de CO 2 et H 2 S dans des solutions aqueuses de diéthanolamine -Dans cet article, nous présentons un équipement expérimental capable de déterminer les solubilités mutuelles du CO 2 et d'H 2 S dans des solutions aqueuses de diéthanolamine. Le propos d'un tel équipe-ment est d'étendre les données expérimentales disponibles à propos de tels systèmes. En effet, la littéra-ture est bien documentée en ce qui concerne les solubilités de CO 2 ou d'H 2 S mais elle est plus réduite pour les mélanges de gaz acides. L'approche expérimentale employée ici est une méthode semisynthétique avec échantillonnage de la phase vapeur et détermination du ratio CO 2 /H 2 S. Nous présentons de nouvelles données à propos du système eau -diéthanolamine -CO 2 -H 2 S et nous les comparons à des données de la littérature au travers d'un modèle thermodynamique rigoureux. Abstract -Simultaneous Solubilities of CO 2 and H 2 S in Diethanolamine Aqueous