Product Separation after Chemical Interesterification of Vegetable Oils with Methyl Acetate. Part I: Vapor–Liquid Equilibrium

Casas, Abraham; Ramos, María Jesús; Pérez, Ángel

doi:10.1021/ie3007903

Cited by 9 publications

(4 citation statements)

References 33 publications

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“…6,7 Their elimination through vacuum distillation cannot be accomplished due to the presence of binary azeotropes of diacetin, monoacetin, and glycerol with triacetin. 8 Consequently, these compounds must be removed from the biodiesel−triacetin mixture using liquid−liquid extraction with water. Triacetin has a water solubility of only 7 g/100 L while glycerol is completely soluble.…”

Section: Introductionmentioning

confidence: 99%

Product Separation after Chemical Interesterification of Vegetable Oils with Methyl Acetate. Part II: Liquid–Liquid Equilibrium

Casas

Ramos

Pérez

2012

Ind. Eng. Chem. Res.

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The aim of this work was the removal of diacetin, monoacetin, and glycerol from biodiesel−triacetin mixtures using liquid−liquid extraction with water. Liquid−liquid equilibrium was predicted using UNIFAC based models for the activity coefficient calculations. These data have been corroborated with experimental information from all possible binary, ternary (water, triacetin, and biodiesel), and overall (diacetin, monoacetin, glycerol, water, triacetin, and biodiesel) mixtures. The experimental determination of the diacetin, monoacetin, and glycerol distribution factor and their selectivity with respect to triacetin allows the operating temperature set at 27.5 °C. After that, it was determined that three washing steps, with a water to feed mixture mass ratio of 0.05 (per stage), were necessary for the effective elimination of these compounds. The final composition of the raffinate phase was 94.6 wt % biodiesel and 5.1 wt % triacetin. The extract phase consisted of a mixture of 59.2 wt % acetins and glycerol and 40.7 wt % water.

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Section: Introductionmentioning

confidence: 99%

Product Separation after Chemical Interesterification of Vegetable Oils with Methyl Acetate. Part II: Liquid–Liquid Equilibrium

Casas

Ramos

Pérez

2012

Ind. Eng. Chem. Res.

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“…Fresh feed entered the process as pure MA and soybean oil, which was modeled as triolein. Following the simulation work of Casas et al, 61 the UNIQUAC thermodynamic model was chosen for all units except those processing pure water, which used steam tables. According to Margarida et al, 22 the most important parameters to verify for components that are not readily available in the Aspen Plus database are the molecular weight (MW), critical temperature (T C ), critical pressure (P C ), normal boiling point (T B ), and acentric factor (ω).…”

Section: Experimental Materials and Procedures Triolein (99%)mentioning

confidence: 99%

“…The bottom product of column D-1 (stream 20) contains the two intermediate compounds, MADG and DAMG, unreacted triolein, and the desired FAME and TA product. Casas et al 61 report that vacuum distillation can be used to remove DAMG from FAME and TA; due to similarities in the boiling points and molecular structure, this work assumes that MADG will also separate from the biodiesel product under similar conditions. Therefore, column D-2 operates at 50 mmHg to separate the unreacted oils (stream 28) from the biodiesel product (stream 27).…”

Section: Representative Process Descriptionmentioning

confidence: 99%

Techno-Economic Analysis of Interesterification for Biodiesel Production

2023

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Interesterification is an alternative reaction for the production of fatty acid alkyl esters from triglycerides, a pathway that avoids unwanted byproduct formation. In this work, the technical and economic feasibility of soybean oil interesterification for biodiesel production on a commercial scale is assessed. The interesterification kinetics of triolein (model soybean oil) and methyl acetate using ferric sulfate as a heterogeneous acid catalyst are experimentally determined, and the results are used to parameterize a kinetic model. Process simulations are developed using Aspen Plus V11 for acid and alkaline heterogeneously catalyzed interesterification plants at varying production rates and methyl acetate-to-oil molar ratios (MAOMRs). At all production capacities and MAOMRs tested, the acid-catalyzed processes are found to have more favorable process energy consumption and profitability metrics compared to the alkaline-catalyzed processes. The most economically promising design operates at a production capacity of 30,000 metric tons/yr and an MAOMR of 10:1 with a net present value of $34 million after 20 years and a biodiesel breakeven price of $0.78/kg. This case has a process energy demand of 35,000 MJ/h, resulting in a process energy ratio of 0.25. This work indicates that interesterification shows commercial viability and is a promising alternative to transesterification for biodiesel production.

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“…Diacetinmonoglycerides can be seen as monoglycerides in which the alcohol groups are connected to acetate groups via an ester linkage. While the removal of this compound has been examined in previous works [2,6], considering it is not typically part of biodiesel, we propose to explore the possibility of retaining it in the biodiesel formulation to understand its effects.…”

Section: Introductionmentioning

confidence: 99%

Effects of Diacetinmonoglycerides and Triacetin on Biodiesel Quality

Casas,

Pérez,

Ramos

2023

Energies

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Triacetin offers a higher added value compared to glycerol and can be obtained during the interesterification reaction between methyl acetate and triglycerides. In the same reaction, diacetinmonoglyceride is produced as an intermediate compound. The objective of this study was to assess whether the biodiesel produced, with varying concentrations of these compounds, meets the requirements established by the EN 14214 and ASTM D6751 standards. To achieve this, several properties were measured, including density, kinematic viscosity, cloud point, pour point, cold filter plugging point, methyl ester content, mono-, di-, triglyceride and total glycerol content, as well as the vacuum distillation curve. These measurements were conducted on mixtures of triacetin, diacetinmonoglyceride, and biodiesel, using different types of biodiesel such as palm, soybean, sunflower and rapeseed. Additionally, the solubility of these ternary mixtures in conventional diesel was evaluated. The results indicated that the EN 14214 standard imposes limits on the density and viscosity of biodiesel, restricting the content of triacetin (up to 5–10% by weight) and diacetinmonoglyceride (up to 3–4% by weight). However, the content of monoglycerides presents the most restrictive condition, as the chromatographic technique used cannot differentiate between monoglycerides and diacetinmonoglycerides. Consequently, their content is limited to a range of 0.15% to 0.70% by weight, depending on the prevailing climate conditions. Similarly, the ASTM D6751 standard sets a limitation of 0.40% by weight for monoglycerides to three out of six grades of biodiesel. Based on the findings of this study, which demonstrate that diacetinmonoglycerides do not have adverse effects on the cold performance of biodiesel, the inclusion of diacetinmonoglycerides in biodiesel production would still necessitate the development of standard test methods capable of differentiating between monoglycerides and diacetinmonoglycerides.

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Product Separation after Chemical Interesterification of Vegetable Oils with Methyl Acetate. Part I: Vapor–Liquid Equilibrium

Cited by 9 publications

References 33 publications

Product Separation after Chemical Interesterification of Vegetable Oils with Methyl Acetate. Part II: Liquid–Liquid Equilibrium

Product Separation after Chemical Interesterification of Vegetable Oils with Methyl Acetate. Part II: Liquid–Liquid Equilibrium

Techno-Economic Analysis of Interesterification for Biodiesel Production

Effects of Diacetinmonoglycerides and Triacetin on Biodiesel Quality

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