Liquid–Liquid Equilibrium Data for the System Lard + Oleic Acid + Ethanol + Water at 318.2 K: Cholesterol Distribution Coefficients

2012 ◽  
Vol 57 (6) ◽  
pp. 1728-1736 ◽  
Author(s):  
Maira G. Granero ◽  
Christianne E. C. Rodrigues ◽  
Cintia B. Gonçalves
Keyword(s):  
Oleic Acid ◽  
Distribution Coefficients ◽  
Liquid Equilibrium ◽  
Equilibrium Data

Liquid−Liquid Equilibrium Data for Fatty Systems Containing Refined Rice Bran Oil, Oleic Acid, Anhydrous Ethanol, and Hexane

2009 ◽  
Vol 54 (8) ◽  
pp. 2174-2181 ◽  
Author(s):  
Wagner L. Priamo ◽  
Marcelo Lanza ◽  
Antonio J. A. Meirelles ◽  
Eduardo A. C. Batista
Keyword(s):  
Oleic Acid ◽  
Rice Bran ◽  
Rice Bran Oil ◽  
Anhydrous Ethanol ◽  
Liquid Equilibrium ◽  
Equilibrium Data

Liquid−Liquid Equilibrium Data for the System Corn Oil + Oleic Acid + Ethanol + Water at 298.15 K

2002 ◽  
Vol 47 (3) ◽  
pp. 416-420 ◽  
Author(s):  
Cintia B. Gonçalves ◽  
Eduardo Batista ◽  
Antonio J. A. Meirelles
Keyword(s):  
Oleic Acid ◽  
Corn Oil ◽  
Liquid Equilibrium ◽  
Equilibrium Data

Application of deep eutectic solvents (DES) to the denitrification of transportation fuels : insights from experimental liquid-liquid phase equilibrium data

2018 ◽  
Author(s):  
◽  
Sanele Enough Msibi
Keyword(s):  
Ethylene Glycol ◽  
Fossil Fuels ◽  
Choline Chloride ◽  
Deep Eutectic Solvent ◽  
Deep Eutectic Solvents ◽  
Distribution Coefficients ◽  
Liquid Equilibrium ◽  
Transportation Fuels ◽  
Basic Nitrogen ◽  
Equilibrium Data

Air pollution by combustion of fossil fuels is of global concern in this decade and beyond. The presence of nitrogen and sulphur impurities pose deleterious effects to refinery equipment, the environment, and human health. Therefore, many governments continue to impose stringent environmental regulations and standards on transportation fuels emissions. The current study evaluates alternate processing solutions to complement or replace the currently used processes to refine these impurities to meet the increasingly stringent fuel standards. This study evaluates the use of a class extractive solvents called Deep Eutectic Solvents (DES) for the removal of basic nitrogen impurities from refining streams by liquid-liquid extraction. This process is evinced as energy saving and environmentally friendly. The removal of pyridine and quinoline by the direct analytical method with choline chloride based deep eutectic solvent (DES) was studied. Liquid-liquid equilibrium measurements data were undertaken at 298.15 K and atmospheric pressure for n-heptane + pyridine/quinoline + [choline chloride + glycerol] DES and n-heptane + pyridine/quinoline + [choline chloride + ethylene glycol] DES systems. The obtained data were then regressed using the Non Random Two Liquid and Universal Quasi-Chemical models activity coefficient, and their mathematical reliability was validated using the Othmer Tobias and Hand correlations. A mixture of choline chloride and glycerol (DES1) showed greater extraction potential for basic nitrogen containing compounds compared to choline chloride and ethylene glycol with a distribution coefficient and selectivity of 22.7 and 2056 for pyridine, and 3.3 and 164.9 for quinoline respectively. The studied solvents showed comparability to organic and ionic liquids solvents in selectivity and distribution coefficients. The obtained liquid-liquid equilibrium data can be used in the design of a solvent extraction equipment, as phase diagrams plays an important role in separation process design.

Liquid−Liquid Equilibrium Data for Systems ContainingJatropha curcasOil + Oleic Acid + Anhydrous Ethanol + Water at (288.15 to 318.15) K

2010 ◽  
Vol 55 (7) ◽  
pp. 2416-2423 ◽  
Author(s):  
César A. S. da Silva ◽  
Guilherme Sanaiotti ◽  
Marcelo Lanza ◽  
Antonio J. A. Meirelles ◽  
Eduardo A. C. Batista
Keyword(s):  
Oleic Acid ◽  
Anhydrous Ethanol ◽  
Liquid Equilibrium ◽  
Equilibrium Data

Liquid-Liquid Equilibrium of the Ternary System Water/Formic Acid/1-Pentanol at T= 308.2 K

2013 ◽  
Vol 3 (2) ◽  
pp. 85-93 ◽  
Author(s):  
Hossein Ghanadzadeh ◽  
Shahin Asan ◽  
Milad Sangashekan
Keyword(s):  
Ternary System ◽  
Formic Acid ◽  
Ambient Pressure ◽  
Distribution Coefficients ◽  
Liquid Equilibrium ◽  
Separation Factors ◽  
Mass Fractions ◽  
Equilibrium Data ◽  
Calculated Mass

Liquid–liquid equilibrium data for the (water + Formic acid + 1-pentanol) ternary system were determined at T = (308.2) K in ambient pressure. This ternary system exhibits type-1 behavior of LLE. Distribution coefficients and separation factors were measured to evaluate the extracting capacity of the solvent. The consistency of the experimental tie-line data was determined through the Othmer–Tobias and Bachman equations. The raw experimental data were correlated using the NRTL and UNIQUAC models. The average root-mean-square deviation between the experimental and calculated mass fractions was 0.488% and 0.465%.

Vapor–Liquid Equilibrium Data for Carbon Dioxide + (R,S)-1,2-Isopropylidene Glycerol (Solketal) + Oleic Acid Systems at High Pressure

2014 ◽  
Vol 59 (5) ◽  
pp. 1494-1498 ◽  
Author(s):  
Andréia Fátima Zanette ◽  
Leandro Ferreira-Pinto ◽  
Willyan Machado Giufrida ◽  
André Zuber ◽  
Andresa Carla Feirhmann ◽  
...  
Keyword(s):  
Carbon Dioxide ◽  
High Pressure ◽  
Oleic Acid ◽  
Liquid Equilibrium ◽  
Vapor Liquid Equilibrium ◽  
Equilibrium Data ◽  
Isopropylidene Glycerol ◽  
Vapor Liquid

scholarly journals LIQUID-LIQUID EQUILIBRIA OF THE WATER+ETHANOL+DIMETHYL ADIPATE TERNARY SYSTEM

2002 ◽  
Vol 10 (11) ◽  
pp. 19-31
Author(s):  
Erol Ince ◽  
S. ismail Kirbaslar
Keyword(s):  
Experimental Data ◽  
Phase Equilibrium ◽  
Distribution Coefficients ◽  
Liquid Equilibrium ◽  
Immiscibility Region ◽  
Separation Factors ◽  
Equilibrium Data ◽  
Dimethyl Adipate ◽  
Tie Line ◽  
System Water

Liquid-liquid equilibrium data for the terna1y system water-ethanol-dimethyl adipate (dibasic ester) have been determined experimentally at 298.15±0.20, 308.15±0.20, and 318.15±0.20 K. Tie-line compositions were correlated by the Othmer-Tobias method. The UNIFAC method was used to predict the phase equilibrium in the system using the interaction parameters determined from experimental data between the CH3, CH2, OH, CH3COO and H20 groups. Distribution coefficients and separation factors were evaluated for the immiscibility region

Isothermal and isobaric vapour-liquid equilibrium data in the tetrachloromethane-sec-butyl alcohol system

1983 ◽  
Vol 48 (9) ◽  
pp. 2446-2453 ◽  
Author(s):  
Jan Linek
Keyword(s):  
Experimental Data ◽  
Boiling Point ◽  
Butyl Alcohol ◽  
Correlation Equations ◽  
Wilson Equation ◽  
Liquid Equilibrium ◽  
Raoult’S Law ◽  
System A ◽  
Equilibrium Data ◽  
Alcohol System

Isothermal vapour-liquid equilibrium data at 65, 73 and 80 °C and isobaric ones at 101.3 kPa were measured in the tetrachloromethane-sec-butyl alcohol system. A modified circulation still of the Gillespie type was used for the measurements. Under the conditions of measurement, the system exhibits positive deviations from Raoult's law and minimum boiling-point azeotropes. The experimental data were fitted to a number of correlation equations, the most suitable being the Wilson equation.

Vapour-liquid equilibrium in the ternary system cyclohexane-acetic acid-propionic acid

1989 ◽  
Vol 54 (11) ◽  
pp. 2840-2847 ◽  
Author(s):  
Ivona Malijevská ◽  
Alena Maštalková ◽  
Marie Sýsová
Keyword(s):  
Acetic Acid ◽  
Ternary System ◽  
Propionic Acid ◽  
Activity Coefficients ◽  
Error Propagation ◽  
Analytical Techniques ◽  
Liquid Equilibrium ◽  
Consistency Test ◽  
Propagation Law ◽  
Equilibrium Data

Isobaric equilibrium data (P = 101.3 kPa) for the system cyclohexane-acetic acid-propionic acid have been measured by two different analytical techniques. Activity coefficients calculated by simultaneous solving of equations for the chemical and phase equilibria were subjected to a consistency test based on inaccuracies determined from the error propagation law, and were correlated by Wilson’s equation. The activity coefficients measured were compared with those calculated from binary vapour-liquid equilibrium data and with values predicted by the UNIFAC method.

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