Vapor–liquid equilibrium of fatty acid ethyl esters determined using DSC

Silva, Luciana Y. Akisawa; Falleiro, Rafael M. Matricarde; Meirelles, Antônio José de Almeida; Krähenbühl, Maria Alvina

doi:10.1016/j.tca.2010.10.002

Cited by 39 publications

(9 citation statements)

References 10 publications

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“…To test the performance of equilibrium apparatus, the VLE data of the mixture of methyl myristate and methyl palmitate was measured at 4.0 kPa. Our experimental data were in good agreement with those reported by Rose and Supina and Akisawa . Table shows the comparison between the literature data and the data obtained by cubic spline interpolation of the data determined in our study.…”

Section: Resultssupporting

confidence: 91%

“… y 1 – x 1 diagram of the methyl myristate and methyl palmitate system at 30 mmHg: ■, experimental values; △, data in ref ; ○, data in ref .…”

Section: Resultsmentioning

confidence: 99%

“…Ceriani and Meirelles proposed a group contribution method for the estimation of the vapor pressure of fatty compounds and gave good agreement with experimental data of fatty mixtures equilibrium with UNIFAC models. Akisawa et al determined the VLE data of fatty acid ethyl esters using differential scanning calorimetry (DSC) and obtained the binary interaction parameters of the Wilson, nonrandom two-liquid (NRTL), and universal quasichemical activity coefficient (UNIQUAC) models. Considering the scarcity of the VLE data of the methyl esters and their importance to the biodiesel industry, methyl palmitate (C 17 H 34 O 2 ) and methyl stearate (C 19 H 38 O 2 ), the major components of biodiesel, would be studied in this study.…”

Section: Introductionmentioning

confidence: 99%

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Isobaric Vapor–Liquid Equilibrium of the Mixture of Methyl Palmitate and Methyl Stearate at 0.1 kPa, 1 kPa, 5 kPa, and 10 kPa

Hou

Ding

et al. 2012

J. Chem. Eng. Data

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Isobaric vapor−liquid equilibrium (VLE) data of the mixture of methyl palmitate and methyl stearate at 0.1 kPa, 1 kPa, 5 kPa, and 10 kPa were measured with a modified Othmer still. Methyl palmitate and methyl stearate were the major components of the biodiesel. The experimental results were correlated with Wilson and nonrandom two-liquid (NRTL) activity coefficient models and were compared with a group contribution model (UNIFAC). The binary interaction parameters of the Wilson and NRTL models were fitted into the experimental data which were obtained at different pressures. The UNIFAC model did not predict the VLE for methyl palmitate and methyl stearate at reduced pressures well. The Wilson and NRTL models could well correlate with the experimental data at 1 kPa, 5 kPa, and 10 kPa. However, for the lower pressure 0.1 kPa, the Wilson model and NRTL model had worse correlatations with our experimental data than the higher pressures. These models could develop VLE calculations of the mixtures and provide guidelines for the separation of components by vacuum distillation.

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Section: Resultssupporting

confidence: 91%

“… y 1 – x 1 diagram of the methyl myristate and methyl palmitate system at 30 mmHg: ■, experimental values; △, data in ref ; ○, data in ref .…”

Section: Resultsmentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

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Isobaric Vapor–Liquid Equilibrium of the Mixture of Methyl Palmitate and Methyl Stearate at 0.1 kPa, 1 kPa, 5 kPa, and 10 kPa

Hou

Ding

et al. 2012

J. Chem. Eng. Data

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“…Nevertheless, despite the recently published extensive work on phase equilibria involved in biodiesel production [7,13,14], VLE information for the biolubricant production operating under low pressure is still lacking. As an illustration, Table 1 [12,[15][16][17][18][19][20] gives an overview of the low-pressure VLE related to biodiesel components that were published over the past 10 years. No similar information was found for biolubricants.…”

Section: Introductionmentioning

confidence: 99%

Phase equilibria of mixtures involving fatty acid ethyl esters and fat alcohols between 4 and 27 kPa for bioproduct production

Roze

Pignat

Ferreira

et al. 2021

Fuel

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The aim of this paper is to bring valuable phase equilibria information for the design and operation of biolubricant and related biofuel product processes. As a result, Vapor-Liquid Equilibrium (VLE) measurements, at different temperatures, pressures and global compositions, for the ternary systems [Ethanol + 2-Ethyl-1-hexanol + 1-Dodecanol] and [Ethanol + 1-Octanol + 1-Dodecanol], as well as a multicomponent system containing these alcohols together with Balanites aegyptiaca fatty acid ethyl esters are reported for the first time (data pressure and temperature ranges: 4394-26790 Pa, 306-423 K). The Dortmund modified UNIFAC model showed very high accuracy in the prediction of these VLE, with overall average absolute deviations on the liquid and vapor molar compositions of 0.007 and 0.0003 for the ternary systems, 0.003 and 0.006 for the multicomponent system.

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“…Model comparisons for FAEE often focus on FAEE mixtures derived from one typical fatty acid source (e.g., Canola biodiesel, Jatropha biodiesel, etc.) instead of pure FAEE components, , or binary interaction parameters of g E models for FAEE mixtures which are relevant for separation processes . Chang et al published recommendations for pure-component property estimation in the course of biodiesel production processes .…”

Section: Introductionmentioning

confidence: 99%

Estimation of Pure-Component Properties of Biodiesel-Related Components: Fatty Acid Ethyl Esters

Wallek

Knöbelreiter

Rarey

2018

Ind. Eng. Chem. Res.

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Common, nonspecialized group-contribution and corresponding-state models for the estimation of normal boiling point, critical data, vapor pressure, liquid density, dynamic viscosity, and surface tension are reviewed in view of their application to fatty acid ethyl esters to provide guidelines for practical application of these models in process engineering. As a result, these properties can be estimated in a satisfactory manner when choosing an appropriate model, showing minimum average absolute mean deviations of the normal boiling point below 5 K (3.4 K for saturated and 4.2 K for unsaturated components), those of the critical temperature below 3 K (2.3 K for saturated and 1.2 K for unsaturated components), those of the critical pressure in the region of 50 kPa (54 kPa for saturated and 2.1 kPa for unsaturated components), and minimum relative mean deviations of saturation pressures from 2% around the normal boiling point to 15% at extremely low pressures, those of liquid density below 1%, those of viscosity at a maximum of 7%, and those of surface tension around 2.4%.

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Vapor–liquid equilibrium of fatty acid ethyl esters determined using DSC

Cited by 39 publications

References 10 publications

Isobaric Vapor–Liquid Equilibrium of the Mixture of Methyl Palmitate and Methyl Stearate at 0.1 kPa, 1 kPa, 5 kPa, and 10 kPa

Isobaric Vapor–Liquid Equilibrium of the Mixture of Methyl Palmitate and Methyl Stearate at 0.1 kPa, 1 kPa, 5 kPa, and 10 kPa

Phase equilibria of mixtures involving fatty acid ethyl esters and fat alcohols between 4 and 27 kPa for bioproduct production

Estimation of Pure-Component Properties of Biodiesel-Related Components: Fatty Acid Ethyl Esters

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