Phase equilibrium measurements and thermodynamic modelling for the systems involving valeric acid, ethanol, ethyl valerate and water plus CO 2

Veiga, Bruno Aguilar; Trancoso, Julia; Luz, Luiz Fernando de Lima; Corazza, Marcos L.

doi:10.1016/j.jct.2017.05.011

Cited by 9 publications

(12 citation statements)

References 35 publications

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“…The general basis of the experimental apparatus and procedure used in this work have been previously reported by our research group. − Briefly, the experimental data measurements were carried out in a high-pressure variable-volume view cell containing a movable piston, which allows pressure control inside the cell. The apparatus also includes a syringe pump (ISCO, model 260D) for injecting CO 2 into the cell and for manipulating pressure into the equilibrium unit, and an electrical heating jacket for the temperature control.…”

Section: Methodsmentioning

confidence: 99%

“…Thermodynamic modeling of the experimental phase equilibrium data measured in this work followed a previously reported procedure, − using the Peng–Robinson equation of state with Boston–Mathias alpha function (PR-BM) , and the conventional quadratic van der Waals mixing rule (vdW2), eqs and . The Boston–Mathias alpha function is given in eq .…”

Section: Thermodynamic Modelingmentioning

confidence: 99%

“…The visual observations were achieved through two sapphire windows, one on the side and another frontal to the cell. For each system composition, the procedure was the same as presented by Veiga et al: 12 flushing the cell with CO 2 (288.15 K and 6.5 MPa) to remove any residual air; loading the cell with the respective amount of liquid solute (EL or LA) and then with the CO 2 (288.15 K and 10 MPa); and setting the pressure to reach the homogeneous phase condition (one phase). At a fixed temperature, the phase transition pressure (the phase saturation condition) was measured by the slow depressurization of the system (using the syringe pump) and read at the incipient new phase formation.…”

Section: Introductionmentioning

confidence: 99%

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Phase Equilibrium Measurements and Thermodynamic Modeling of the Systems (CO₂ + Ethyl Levulinate) and (CO₂ + Levulinic Acid)

et al. 2019

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This work reports phase equilibrium measurements and thermodynamic modeling of the binary systems (CO 2 + ethyl levulinate) and (CO 2 + levulinic acid). Each composition was carried out in a high-pressure variablevolume view cell at temperatures ranging from 303.15 to 353.15 K and with CO 2 mole fraction ranging from 0.4002 to 0.9751 for the system (CO 2 + ethyl levulinate) and from 0.4083 to 0.9930 for the system (CO 2 + levulinic acid). Under these conditions, only vapor−liquid phase transitions were observed. The experimental data were modeled with the Peng−Robinson cubic equation of state with the Boston− Mathias alpha function (PR-BM) and using the van der Waals quadratic mixing rule. The results showed that the experimental data of the system (CO 2 + ethyl levulinate) were adequately represented by the thermodynamic model with a unique set of binary interaction parameters, which were fitted from all isotherms. Whereas the experimental data of the system (CO 2 + levulinic acid) were only adequately represented with temperature-dependent binary interaction parameters.

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Section: Methodsmentioning

confidence: 99%

Section: Thermodynamic Modelingmentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

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Phase Equilibrium Measurements and Thermodynamic Modeling of the Systems (CO₂ + Ethyl Levulinate) and (CO₂ + Levulinic Acid)

et al. 2019

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“…The experimental apparatus and procedure used in this work were presented and described in previous publications [13][14][15][16][17]. Briefly, the experimental data measurements were performed in a high-pressure variable-volume view cell containing a movable piston, which allows the pressure control inside the cell.…”

Section: Apparatus and Experimental Proceduresmentioning

confidence: 99%

Phase equilibrium measurements and thermodynamic modeling of {CO2 + diethyl succinate + cosolvent} systems

Petza

Grilla

Capeletto

et al. 2019

Fluid Phase Equilibria

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This work reports experimental phase equilibrium data for the binary systems {CO2(1) + diethyl succinate(2)} and {CO2(1) + ethyl acetate(2)}, and for the ternary systems {CO2(1) + diethyl succinate(2) + ethanol(3)} and {CO2(1) + diethyl succinate(2) + ethyl acetate(3)}.The experiments for the binary system {CO2(1) + diethyl succinate(2)} were carried out at temperatures ranging from 308 K to 358 K, and temperatures ranging from 303 K to 343 K for {CO2(1) + ethyl acetate(2)} as well as for all ternary systems. Only vapor-liquid equilibria were observed for all systems. The experimental measurements were carried out in a high-pressure variable-volume view cell containing a movable piston, which allows pressure control inside the cell. Binary and ternary systems were modeled with the Peng-Robinson cubic equation of state with the van der Waals quadratic mixing rule (vdW2).The presence of a cosolvent (ethanol and ethyl acetate) decreased the saturation pressures of either bubble or dew points compared to the binary system CO2 + diethyl succinate, increasing the solubility of diethyl succinate in CO2.

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“…The total component splitting of the azeotrope solution requires the addition of a ternary solute, which changes the behavior of the liquid vapor in the distillation column. Several liquid and solid ternary solute materials can be used in ethanol dehydration, including benzene, pentane, furfural, ethylene glycol, diethyl ether, toluene, glycerol, salt, and ionic liquids (ILs) [13][14][15][16][17][18]. At the industrial scale, ILs offer the greatest potential in extractive distillation.…”

Section: Introductionmentioning

confidence: 99%

Dehydrating Ethanol Using a Ternary Solute and Extractive Batch Distillation

Marnoto

Budiaman

Hapsari

et al. 2019

MJAS

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Anhydrous bioethanol is a material used in many applications including biofuel. Commonly, bioethanol is produced through sugar fermentation which results in a low concentration of ethanol. For utilization as biofuel, the lowest ethanol concentration should be 99.5%. Distillation is common technique to dry a mixture solution, however, the mixture of bioethanol and water is forming an azeotrope that limit the concentration of 96% ethanol. This paper discusses ethanol dehydration through extractive batch distillation by the addition of a ternary solute sodium hydroxide, citric acid, sulfuric acid, glycerol or ethylene glycol to ethanol. The initial concentration of ethanol used was 86% v/v, and the amount of ternary solute added was selected based on the colligative properties of the solution, which included a boiling point elevation (ΔT B) that ranged from 5 to 25 °C. All the ternary solutes could break or shift the ethanol-water azeotrope. The highest concentration of ethanol was 99.91% v/v at ΔT B = 25 °C with sulfuric acid as the ternary component. The resulted ethanol concentration exhibited a linear relationship with ΔT B , which was also affected by the boiling point of the ternary solute. This study successfully produced anhydrous bioethanol by low cost and simple distillation process.

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Phase equilibrium measurements and thermodynamic modelling for the systems involving valeric acid, ethanol, ethyl valerate and water plus CO 2

Cited by 9 publications

References 35 publications

Phase Equilibrium Measurements and Thermodynamic Modeling of the Systems (CO₂ + Ethyl Levulinate) and (CO₂ + Levulinic Acid)

Phase Equilibrium Measurements and Thermodynamic Modeling of the Systems (CO₂ + Ethyl Levulinate) and (CO₂ + Levulinic Acid)

Phase equilibrium measurements and thermodynamic modeling of {CO2 + diethyl succinate + cosolvent} systems

Dehydrating Ethanol Using a Ternary Solute and Extractive Batch Distillation

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Phase equilibrium measurements and thermodynamic modelling for the systems involving valeric acid, ethanol, ethyl valerate and water plus CO 2

Cited by 9 publications

References 35 publications

Phase Equilibrium Measurements and Thermodynamic Modeling of the Systems (CO2 + Ethyl Levulinate) and (CO2 + Levulinic Acid)

Phase Equilibrium Measurements and Thermodynamic Modeling of the Systems (CO2 + Ethyl Levulinate) and (CO2 + Levulinic Acid)

Phase equilibrium measurements and thermodynamic modeling of {CO2 + diethyl succinate + cosolvent} systems

Dehydrating Ethanol Using a Ternary Solute and Extractive Batch Distillation

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Product

Resources

About

Phase Equilibrium Measurements and Thermodynamic Modeling of the Systems (CO₂ + Ethyl Levulinate) and (CO₂ + Levulinic Acid)

Phase Equilibrium Measurements and Thermodynamic Modeling of the Systems (CO₂ + Ethyl Levulinate) and (CO₂ + Levulinic Acid)