Experimental screening of ionic liquids as mass agents in the n-hexane/1-hexene extractive distillation

Ayuso, Miguel; Varela, Jorge J.; García-Somoza, Noelia; García, Julián; Rodrı́guez, Francisco

doi:10.1016/j.fluid.2021.113205

Cited by 7 publications

(6 citation statements)

References 49 publications

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“…On the contrary, the greater the relative volatility of the system is, the lower is the energy consumption of the separation process. The relative volatility of (−)-α-pinene (1) to (−)-β-pinene (2) (α 12 ) is calculated as follows: α 12 = true y 1 x 1 true y 2 x 2 where x 1 and x 2 denote the liquid phase molar fractions of (−)-α-pinene (1) and (−)-β-pinene (2), respectively, and y 1 and y 2 denote the vapor phase molar fractions of (−)-α-pinene (1) and (−)-β-pinene (2), respectively.…”

Section: Resultsmentioning

confidence: 99%

Measurement and Correlation of Isothermal Vapor–Liquid Equilibrium Data for (−)-α-Pinene + (−)-β-Pinene + Water + Phenoxyacetic Acid

Wei

Chen

Wang

et al. 2023

Ind. Eng. Chem. Res.

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Isothermal vapor–liquid equilibrium data of the binary system (−)-α-pinene + (−)-β-pinene and the quaternary system (−)-α-pinene + (−)-β-pinene + water + phenoxyacetic acid were measured at 313.2, 323.2, and 333.2 K using headspace gas chromatography. The experimental data showed that the addition of phenoxyacetic acid and water promoted the separation of (−)-α-pinene and (−)-β-pinene. The experimental data were correlated using the UNIQUAC and NRTL models. The two models showed good correlation for the binary system, whereas the UNIQUAC model gave more accuracy for the quaternary system. Moreover, the COSMO-RS model can be an efficacious method for predicting VLE data of the determined binary and quaternary systems. In addition, the optimal spatial configuration and binding energy between the molecules were obtained by DFT, and the effects on (−)-α-pinene and (−)-β-pinene with the addition of phenoxyacetic acid and water were discussed on the molecular scale.

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Section: Resultsmentioning

confidence: 99%

Measurement and Correlation of Isothermal Vapor–Liquid Equilibrium Data for (−)-α-Pinene + (−)-β-Pinene + Water + Phenoxyacetic Acid

Wei

Chen

Wang

et al. 2023

Ind. Eng. Chem. Res.

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“…ED is a prevalent method for azeotropic separation. 62 By using the proper entrainer, this process elevates the relative volatility of the separated components. 63 ED combines the advantages of extraction 64 and distillation, 65 demonstrating unique benefits in areas such as energy consumption reduction and separation efficiency.…”

Section: ■ Extractive Distillation Process Designmentioning

confidence: 99%

“…Guo et al conducted vapor–liquid equilibrium experiments to predict the phase equilibrium behavior between components and entrainers, and efficiently separated the azeotropic system. Ayuso et al designed the ED process and used experimental methods to select suitable ILs as entrainers for the separation of azeotropic systems. The combination of simulation and experiment can provide a reliable basis for simulation results, improve the accuracy of the simulated process, and provide a guarantee for the application of the designed process in real production.…”

Section: Analysis Of Entrainer and Azeotropic Mechanismmentioning

confidence: 99%

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Design and Multiple Performance Evaluation of Green Sustainable Process for Azeotropes Separation via Extractive Distillation

Zhong,

Cheng,

Dai

et al. 2023

ACS Sustainable Chem. Eng.

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Multicomponent liquid mixtures, particularly azeotropes, are extensively utilized in the chemical, petroleum, pharmaceutical, and other processing industries. Energy-saving and efficient separation of azeotropes holds significant value for the design and development of sustainable industrial processes. Extractive distillation (ED) has consistently played a pivotal role in azeotrope separation. We offer a broad and comprehensive review that encompasses recent progress in multiple aspects of ED, including the screening of entrainers, process design, enhancement schemes, dynamic control strategies, and environmental assessment. Initially, we delved into the application of quantum chemistry calculations and molecular dynamics simulation for screening suitable entrainers. We then elucidate the design principles and forms of two distinct types of ED processes. Subsequently, we explore the intensification mechanisms of the ED process through coupling mechanisms, such as heat integration and the combination of ED with other distillation processes. We also summarize the recent improvements in dynamic control strategies for various ED processes. Lastly, we evaluate various aspects of ED from the perspectives of environmental impact, economic viability, and exergy analysis. This study investigates the challenges, prospects, and emerging trends of ED technology for the separation of multicomponent azeotropes.

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“…The economic advantages of the IL extractive distillation process and its heat pump version were revealed. [18][19][20] Undiluted ILs were used to separate precious and base metals by Vereycken et al 21 An IL extractant was designed and optimized for the separation of phenyl-n-propanol, based on the assessment of the separation performance of ILs according to the annual cost of the extraction distillation process by Li et al [22][23][24] Solubility and selectivity calculated by COSMOthermX software have often been used to select ILs. 22,[25][26][27][28][29][30][31] Selectivities and solubilities of 676 common ILs were calculated for the separation of a benzenen-propanol mixture using COSMOthermX software.…”

Section: Introductionmentioning

confidence: 99%

Extractive distillation of tetrahydrofuran–ethanol azeotropic mixture with ionic liquid as extractant

Li,

Zhang,

Guo

et al. 2023

J of Chemical Tech & Biotech

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BACKGROUNDThe tetrahydrofuran‐ethanol azeotrope can't be separated by common distillation, but can be effectively separated by extractive distillation. Extractive distillation can be simulated by Aspen Plus software. Minimum annual cost of the process can be calculated to assess ionic liquid separation ability. The interaction energy can be used to explain the separation mechanism.RESULTSThe non‐random two‐liquid model parameters of the ternary mixtures for tetrahydrofuran and ethanol containing tributyl methylammonium acetate or 1‐octyl‐3‐methylimidazolium acetate were obtained. Thermodynamic properties databases of tributyl methylammonium acetate, 1‐hexyl‐2,3‐dimethylimidazolium acetate and 1‐octyl‐3‐methylimidazolium acetate were established. Based on the thermodynamic model parameters and properties, the sequential iterative method was used to gain the best operating conditions and minimum total annual cost the of extractive distillation process. The interaction energy was calculated to explain the separation mechanism.CONCLUSIONSThe separation performance of tributyl methylammonium acetate is better than that of 1‐hexyl‐2,3‐dimethylimidazolium acetate or 1‐octyl‐3‐methylimidazolium acetate. The selection and design of the ILs can be operated by the interaction energy.This article is protected by copyright. All rights reserved.

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Experimental screening of ionic liquids as mass agents in the n-hexane/1-hexene extractive distillation

Cited by 7 publications

References 49 publications

Measurement and Correlation of Isothermal Vapor–Liquid Equilibrium Data for (−)-α-Pinene + (−)-β-Pinene + Water + Phenoxyacetic Acid

Measurement and Correlation of Isothermal Vapor–Liquid Equilibrium Data for (−)-α-Pinene + (−)-β-Pinene + Water + Phenoxyacetic Acid

Design and Multiple Performance Evaluation of Green Sustainable Process for Azeotropes Separation via Extractive Distillation

Extractive distillation of tetrahydrofuran–ethanol azeotropic mixture with ionic liquid as extractant

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