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Journal articles on the topic 'Azeotrope'

Author: Grafiati

Published: 4 June 2021

Last updated: 18 February 2022

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1

Tien Thi, Luot. "ENTRAINER SELECTION FOR SEPARATION OF AZEOTROPIC MIXTURES BY DISTILLATION METHODS." Vietnam Journal of Science and Technology 56, no. 4A (October 19, 2018): 89. http://dx.doi.org/10.15625/2525-2518/56/4a/12952.

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Azeotropic or close – boiling mixtures often preclude conventional distillation as a method of separation. Instead, extractive or azeotropic distillations are commonly used to separate azeotropic or close – boiling mixtures. For the design of those separation units, selecting suitable entrainers (solvents) is a key step. The traditional method for solving this problem is to use experimentation which is time – consuming and expensive. Currently available selection criteria are inadequate. They contradict one another and often lead to incorrect conclusions. Indeed, for a minimum boiling azeotrope, the existing entrainer selection rules state that one should use a high boiling component that introduces no additional azeotrope (Benedict & Rubin, 1945), an intermediate boiling component that introduces no additional azeotrope (Hoffman, 1964), a component which introduces no distillation boundary between the azeotropic constituents (Doherty & Caldarola, 1985), and either a low boiling component that introduces no additional azeotrope or a component that introduces new minimum boiling azeotrope (Stichlmaric, Fair & Bravo, 1989).In this work, Aspen Plus simulator was used to propose an entrainer selection procedure based on the criteria: 1) A good entrainer is a component that eliminates the azeotrope easily (i.e. even when it’s concentration is small). 2) A component that yields high relative volatilities αAB between the two azeotrope constituents.

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2

Valentini, Federica, and Luigi Vaccaro. "Azeotropes as Powerful Tool for Waste Minimization in Industry and Chemical Processes." Molecules 25, no. 22 (November 12, 2020): 5264. http://dx.doi.org/10.3390/molecules25225264.

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Aiming for more sustainable chemical production requires an urgent shift towards synthetic approaches designed for waste minimization. In this context the use of azeotropes can be an effective tool for “recycling” and minimizing the large volumes of solvents, especially in aqueous mixtures, used. This review discusses the implementation of different kinds of azeotropic mixtures in relation to the environmental and economic benefits linked to their recovery and re-use. Examples of the use of azeotropes playing a role in the process performance and in the purification steps maximizing yields while minimizing waste. Where possible, the advantages reported have been highlighted by using E-factor calculations. Lastly azeotrope potentiality in waste valorization to afford value-added materials is given.

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3

Mahdi, Taha, Arshad Ahmad, Mohamed M. Nasef, and Adnan Ripin. "Simulation and Analysis of Process Behavior of Ultrasonic Distillation System for Separation Azeotropic Mixtures." Applied Mechanics and Materials 625 (September 2014): 677–79. http://dx.doi.org/10.4028/www.scientific.net/amm.625.677.

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The performance of an ultrasonic distillation (USD) system is evaluated in Aspen Plus simulation environment. To facilitate the flowsheet development, a mathematical model of a single stage USD developed using Aspen Custom Modeler software is exported to Aspen Plus process simulator. As a case study, the separation of ethanol-ethyl acetate mixture that is known to form azeotrope 55 mole % of ethyl acetate at minimum boiling point of 71.8oC is considered. Simulation results revealed the achievable purity of ethyl acetate of 99 mole % from azeotropic mixture, thus reinforcing the anticipated potentials of sonication phenomena in intensifying distillation process to overcome azeotropes.

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4

Platt, Gustavo Mendes, Marcelo Escobar Aragão, Fernanda Cabral Borges, and Douglas Alves Goulart. "Evaluation of a New Multimodal Optimization Algorithm in Fluid Phase Equilibrium Problems." Ingeniería e Investigación 40, no. 1 (January 1, 2020): 27–33. http://dx.doi.org/10.15446/ing.investig.v40n1.78822.

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Multimodal optimization problems are commonly found in engineering problems, and their solution can be very challenging for metaheuristic approaches. In this work, the use of a recently proposed multimodal metaheuristic method was analyzed - the Multimodal Flower Pollination Algorithm - in two fluid phase equilibrium problems: (i) the calculation of double azeotropes and (ii) parameter estimation in a thermodynamic model. Two different formulations were also considered in the double azeotropy problem. In the azeotrope calculation, a statistical analysis was conducted in order to verify if the algorithm performance is affected by the the problem formulation. The computational results indicate that the methodology provides robust results and that the objective function employed affects the computational performance.

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5

Mahdi, Taha, Arshad Ahmad, Adnan Ripin, Mohamed Mahmoud Nasef, and Olagoke Oladokun. "Aspen Plus Simulation of Ultrasound Assisted Distillation for Separating Azeotropic Mixture." Advanced Materials Research 1113 (July 2015): 710–14. http://dx.doi.org/10.4028/www.scientific.net/amr.1113.710.

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Earlier works have proved the potentials of altering the vapor liquid equilibrium of azeotropic mixture by sonication phenomena. In this work a mathematical model of a single stage vapor-liquid equilibrium system developed in Aspen Custom Modeler is exported to Aspen Plus to represent one stage of ultrasonic flash distillation (USF). The USF modules are connected serially to mimic a distillation process. As a case study, the separation of ethanol-ethyl acetate mixture is considered. The final targeted composition of 99 mole % of ethyl acetate was achieved when 27 USF modules were used despite the fact that the mixture form azeotrope at 55 mole % ethyl acetate. The results reinforced the anticipated potentials of sonication phenomena in intensifying distillation process to overcome azeotropes, and provide useful insights for the development of a pilot-scaled facility that is currently under development.

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6

Fan, Zhi Dong, Xu Bin Zhang, Lu Yang Zhao, Wang Feng Cai, and Fu Min Wang. "Study on the Separation of Azeotrope of Tetrahydrofuran-Water Using a Combined Method of Extractive and General Distillation." Advanced Materials Research 803 (September 2013): 149–52. http://dx.doi.org/10.4028/www.scientific.net/amr.803.149.

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As an important solvent, tetrahydrofuran has broad applications. Due to its process of production, water will be mixed into the product and should be removed. However, tetrahydrofuran will form a minimum boiling azeotrope with water, which has a boiling point of 63.4°C, so general distillation can not separate them. Common methods to solve this include extractive distillation, pressure swing distillation, azeotropic distillation, pervaporation and so on. In this experiment, we coupled extractive distillation and general distillation, selecting ethylene glycol as the extractant, and successfully dehydrated the azeotrope. The mass fraction of water is reduced from 18% to less than 500ppm,which matches the requirement.

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7

Wang, Xue Hui, Tian Nian Zhou, Q. P. Chen, Jin Fei Zhao, Chao Ding, and Jian Wang. "Burning Characteristics of Azeotropic Binary Blended Fuel Pool Fire." Key Engineering Materials 775 (August 2018): 365–70. http://dx.doi.org/10.4028/www.scientific.net/kem.775.365.

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A series of experiments were conducted to investigate the burning characteristics of blended fuel pool fires. The azeotropic binary mixtures blended by ethanol and n-Heptane were selected as blended fuel in experiment. The fuel temperature, fire behaviors, burning rate and flame radiation were recorded in experiments. The result show that azeotropism play an important role in the burning process, the fuel temperature was decrease and the burning rate was increased. The flame radiant fraction of azeotrope has proportional relation with the radiation faction of component.

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8

Milojevic, Svetomir. "Separation processes, I: Azeotropic rectification." Chemical Industry 59, no. 5-6 (2005): 141–50. http://dx.doi.org/10.2298/hemind0506141m.

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In a series of two articles, the problems of azeotrope separation (part I) and the design of separation units (part II) were analyzed. The basic definition and equations of vapour-liquid equilibria for ideal and non-ideal systems, the importance of the activity coefficient calculation necessary for the analysis of non-ideal equilibrium systems, as well as theoretical aspects of azeotrope rectification and the determination of the optimal third component (modifier or azeotrope agent) are presented in the first part.

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9

Zhang, Wen Lin, Nan Meng, Ru Yi Sun, and Chun Li Li. "Isobaric Vapor-Liquid Equilibria of Hexamethyl Disiloxane + Ethyl Acetate System at Normal Pressure." Advanced Materials Research 396-398 (November 2011): 968–72. http://dx.doi.org/10.4028/www.scientific.net/amr.396-398.968.

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Vapor-liquid equilibrium data of hexamethyl disiloxane + ethyl acetate system at 101.3kPa were measured by using double circulating vapor-liquid equilibrium still. The thermodynamic consistency of the VLE data was examined by Herrington method. Experimental data was correlated by NRTL and UNIQUAC parameter models. Both of the models satisfactorily correlated with the VLE data. The result showed that the NRTL model was the most suitable one to represent experimental data satisfactorily and the system had a minimum temperature azeotrope at 350.31 K and the mole azeotropic composition was 0.0330.

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10

Kim, Y. J., and K. H. Simmrock. "AZEOPERT: An expert system for the prediction of azeotrope formation—I. Binary azeotropes." Computers & Chemical Engineering 21, no. 1 (September 1997): 93–111. http://dx.doi.org/10.1016/0098-1354(95)00249-9.

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11

Song, W., R. S. Huss, M. F. Doherty, and M. F. Malone. "Discovery of a reactive azeotrope." Nature 388, no. 6642 (August 1997): 561–63. http://dx.doi.org/10.1038/41515.

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12

Bai, Fang, Chao Hua, and Jing Li. "Separation of Benzene-Cyclohexane Azeotropes Via Extractive Distillation Using Deep Eutectic Solvents as Entrainers." Processes 9, no. 2 (February 12, 2021): 336. http://dx.doi.org/10.3390/pr9020336.

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The separation of benzene and cyclohexane azeotrope is one of the most challenging processes in the petrochemical industry. In this paper, deep eutectic solvents (DES) were used as solvents for the separation of benzene and cyclohexane. DES1 (1:2 mix of tetrabutylammonium bromide (TBAB) and levulinic acid (LA)), DES2 (1:2 mix of TBAB and ethylene glycol (EG)) and DES3 (1:2 mix of ChCl (choline chloride) and LA) were used as entrainers, and vapor-liquid equilibrium (VLE) measurements at atmospheric pressure revealed that a DES comprised of a 2:1 ratio of LA and TBAB could break this azeotrope with relative volatility (αij) up to 4.763. Correlation index suggested that the NRTL modelling approach fitted the experimental data very well. Mechanism of extractive distillation gained from FT-IR revealed that with hydrogen bonding and π–π bond interactions between levulinic acid and benzene could be responsible for the ability of this entrainer to break the azeotrope.

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13

Shi, Xiu Min, and Min Wang. "Vapor-Liquid Equilibria for the Ternary System Ethyl Acetate-Acetonitrile-1-Octyl-3-Methylimidazolium Tetrafluoroborate." Advanced Materials Research 791-793 (September 2013): 141–44. http://dx.doi.org/10.4028/www.scientific.net/amr.791-793.141.

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In order to research the possibility of separating the azeotrope of ethyl acetate + acetonitrile with ionic liquid as the extractant. Isobaric vapor-liquid equilibria for the ternary system ethyl acetate + acetonitrile + 1-octyl-3-methylimidazolium tetrafluoroborate ([OMIBF4) were measured at 101.32 kPa using a recirculation still. The results showed that the VLE of the ternary system was different from that of the binary system. The ionic liquid (IL) studied showed a slight crossover salt effect, which changed the relative volatility of ethyl acetate to acetonitrile and eliminated the azeotropic point when the mole fraction of IL in the liquid phase was greater than 0.05. Therefore, [OMIBF4 can be used as the extractant of extractive distillation for ethyl acetate + acetonitrile system, the suitable mole fraction of [OMIBF4 is about 10%.

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14

Lee, Jae W., Steinar Hauan, and Arthur W. Westerberg. "Circumventing an Azeotrope in Reactive Distillation." Industrial & Engineering Chemistry Research 39, no. 4 (April 2000): 1061–63. http://dx.doi.org/10.1021/ie990447k.

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15

Bento, Jennifer L., Drona R. Madugula, Chetan C. Hire, and Douglas H. Adamson. "Azeotrope enabled polymerization of ethylene oxide." RSC Advances 6, no. 97 (2016): 94459–66. http://dx.doi.org/10.1039/c6ra22064a.

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We report a synthetic route for poly(ethylene oxide) (PEO) using azeotropic distillation to remove water and drive the equilibrium of an alkyl hydroxide and potassium hydroxide to potassium alkoxide, avoiding the use of pyrophoric organometallics.

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16

Loccufier, Eva, Jozefien Geltmeyer, Lode Daelemans, Dagmar R. D'hooge, Klaartje De Buysser, and Karen De Clerck. "Azeotrope Separation: Silica Nanofibrous Membranes for the Separation of Heterogeneous Azeotropes (Adv. Funct. Mater. 44/2018)." Advanced Functional Materials 28, no. 44 (October 2018): 1870313. http://dx.doi.org/10.1002/adfm.201870313.

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17

Hadj-Kali, M. K., V. Gerbaud, and X. Joulia. "AZEOTROPE PREDICTION BY MONTE CARLO MOLECULAR SIMULATION." Chemical Engineering Communications 199, no. 5 (May 2012): 673–88. http://dx.doi.org/10.1080/00986445.2011.616247.

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18

Kalman, S., M. Bengtsson, and D. Lindmark. "Minimum alveolar concentration of halothanediethyl-ether azeotrope." Acta Anaesthesiologica Scandinavica 35, no. 3 (April 1991): 190–95. http://dx.doi.org/10.1111/j.1399-6576.1991.tb03271.x.

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19

Kalman, S. "Studies on the halothane-diethyl-ether azeotrope." Acta Anaesthesiologica Scandinavica 39, no. 3 (April 1995): 416. http://dx.doi.org/10.1111/j.1399-6576.1995.tb04089.x.

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20

Shorr, L. M. "A correlation method for binary azeotrope data." Journal of Applied Chemistry 14, no. 9 (May 4, 2007): 376–82. http://dx.doi.org/10.1002/jctb.5010140903.

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21

Klein, A., J. U. Repke, and G. Wozny. "Trennung homogener Azeotrope mittels Zweidruck-Batch-Rektifikation." Chemie Ingenieur Technik 78, no. 9 (September 2006): 1283–84. http://dx.doi.org/10.1002/cite.200650392.

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22

Fullarton, Douglas, and Ernst-Ulrich Schlünder. "Diffusionsdestillation - ein neues Trennverfahren für azeotrope Gemische." Chemie Ingenieur Technik 58, no. 5 (1986): 398–400. http://dx.doi.org/10.1002/cite.330580509.

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23

Wang, Qi, Genghua Chen, and Shijun Han. "Determination of ternary azeotrope at subatmospheric pressures." Fluid Phase Equilibria 101 (October 1994): 259–66. http://dx.doi.org/10.1016/0378-3812(94)02547-9.

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24

Lastari, Fonny, Vishnu Pareek, Mark Trebble, Moses O. Tade, Daniel Chinn, Nancy C. Tsai, and Kaman I. Chan. "Extractive distillation for CO2–ethane azeotrope separation." Chemical Engineering and Processing: Process Intensification 52 (February 2012): 155–61. http://dx.doi.org/10.1016/j.cep.2011.10.001.

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25

Vahdat, Nader, and Glenn A. Sather. "Prediction of multicomponent azeotrope composition and temperature." Chemical Engineering Journal 31, no. 2 (October 1985): 83–96. http://dx.doi.org/10.1016/0300-9467(85)80047-2.

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26

Ding, Xin, Xiaohong Wang, Peng Du, Zenghu Tian, and Jingxuan Chen. "Prediction of New Distillation-Membrane Separation Integrated Process with Potential in Industrial Application." Processes 9, no. 2 (February 9, 2021): 318. http://dx.doi.org/10.3390/pr9020318.

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In this paper, a new integrated distillation-membrane separation process solution strategy based on genetic programming (GP) was established for azeotrope separation. Then, a price evaluation method based on the theory of unit membrane area was proposed, so that those membranes which are still in the experimental stage and have no actual industrial cost for reference can also be used in the experimental research. For different characteristics and separation requirements of various azeotropic systems, the solution strategy can be matched with difference pervaporation membranes, and the optimal distillation-membrane separation integrated process can be solved quickly and accurately. Taking methanol-toluene as an example, the separation operation was optimized by using the algorithm. The effects of different feed flows and compositions on the modification of the chitosan membrane were discussed. These results provide a reliable basis for the prospects for development and modification direction of membrane materials which are still in the experimental research stage.

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27

Guldin, Stefan, Morgan Stefik, Hiroaki Sai, Ulrich Wiesner, and Ullrich Steiner. "Controlling the coassembly of highly amphiphilic block copolymers with a hydrolytic sol by solvent exchange." RSC Advances 5, no. 29 (2015): 22499–502. http://dx.doi.org/10.1039/c5ra00836k.

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Block copolymer co-assembly of TiO₂ is facilitated by the introduction of a redissolution step in an azeotrope solvent mixture, allowing the formation of self-assembled cylindrical, lamellar and hexagonal ceramic morphologies.

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28

Zhao, Lei, Xinyu Lyu, Wencheng Wang, Jun Shan, and Tao Qiu. "Comparison of heterogeneous azeotropic distillation and extractive distillation methods for ternary azeotrope ethanol/toluene/water separation." Computers & Chemical Engineering 100 (May 2017): 27–37. http://dx.doi.org/10.1016/j.compchemeng.2017.02.007.

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29

Hu, Jianhua, Charles A. Haynes, Amy HY Wu, Candy MW Cheung, Mark M. Chen, Eric GM Yee, Takehiko Ichioka, Keiko Nishikawa, Peter Westh, and Yoshikata Koga. "Chemical potential and concentration fluctuation in some aqueous alkane-mono-ols at 25oC." Canadian Journal of Chemistry 81, no. 2 (February 1, 2003): 141–49. http://dx.doi.org/10.1139/v03-007.

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Vapour pressures of binary aqueous solutions of methanol, ethanol, 1-propanol, 2-propanol, 1-butanol, and 1-hexanol were measured at 25.00oC in small compositional increments over the entire compositional range. Without resorting to any fitting function, the partial pressures were calculated numerically by methods based on the GibbsDuhem relation. When the system had an azeotrope, near which the numerical methods caused large errors, a graphical readjustment was applied such that the concentration fluctuation, SXX(0) = RT(1 xAL)/([Formula: see text]µ EAL/[Formula: see text]xAL), connected smoothly across the azeotrope. Values of SXX(0) from scattering experiments were also used as a guide for the readjustment procedure. Hence, we report here chemical potential data free from any model or any fitting function.Key Words: aqueous mono-ols, partial pressures by the Boissonnas method, concentration fluctuations.

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30

Rasina, Dace, Aurora Lombi, Stefano Santoro, Francesco Ferlin, and Luigi Vaccaro. "Searching for novel reusable biomass-derived solvents: furfuryl alcohol/water azeotrope as a medium for waste-minimised copper-catalysed azide–alkyne cycloaddition." Green Chemistry 18, no. 23 (2016): 6380–86. http://dx.doi.org/10.1039/c6gc01941b.

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Herein we report the first application of the furfuryl alcohol/water azeotrope as a sustainable and easily recoverable reaction medium for organic chemistry. As first applicantion we have defined a waste-oinimized protocol for click-chemistry synthesi of 1,2,3-triazoles.

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31

Shi, Puyun, Yangchen Gao, Jingyu Wu, Dongmei Xu, Jun Gao, Xiaolong Ma, and Yinglong Wang. "Separation of azeotrope (2,2,3,3-tetrafluoro-1-propanol + water): Isobaric vapour-liquid phase equilibrium measurements and azeotropic distillation." Journal of Chemical Thermodynamics 115 (December 2017): 19–26. http://dx.doi.org/10.1016/j.jct.2017.07.019.

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32

Luyben, William L. "Methanol/Trimethoxysilane Azeotrope Separation Using Pressure-Swing Distillation." Industrial & Engineering Chemistry Research 53, no. 13 (March 21, 2014): 5590–97. http://dx.doi.org/10.1021/ie500043c.

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33

Kalman, S. H., M. Bengtsson, and J. Mårtensson. "Liver function and halothane-diethyl-ether azeotrope anaesthesia." Acta Anaesthesiologica Scandinavica 39, no. 1 (January 1995): 34–38. http://dx.doi.org/10.1111/j.1399-6576.1995.tb05589.x.

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34

Ulrich, Jan, and Manfred Morari. "Homogene azeotrope Rektifikation: Untersuchung der Regelung von Kolonnensequenzen." Chemie Ingenieur Technik 72, no. 9 (September 2000): 960–61. http://dx.doi.org/10.1002/1522-2640(200009)72:9<960::aid-cite9602>3.0.co;2-n.

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35

Sanchez-Segado, Sergio, María José Salar-García, Víctor Manuel Ortiz-Martínez, Antonia Pérez de los Ríos, Francisco José Hernández-Fernández, and Luis Javier Lozano-Blanco. "Evaluation of Ionic Liquids as In Situ Extraction Agents during the Alcoholic Fermentation of Carob Pod Extracts." Fermentation 5, no. 4 (October 18, 2019): 90. http://dx.doi.org/10.3390/fermentation5040090.

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Anhydrous ethanol is a promising alternative to gasoline in fuel engines. However, since ethanol forms an azeotrope with water, high-energy-consumption separation techniques such as azeotropic distillation, extractive distillation, and molecular sieves are needed to produce anhydrous ethanol. This work discusses the potential development of an integrated process for bioethanol production using ionic liquids and Ceratonia siliqua as a carbohydrate source for further fermentation of the aqueous extracts. A four-stage counter-current system was designed to improve the sugar extraction yield to values close to 99%. The alcoholic fermentation of the extracts showed ethanol concentrations of 95 g/L using the microorganism Saccharomyces cerevisae. The production of anhydrous ethanol through extractive distillation with ethylene glycol was simulated using CHEMCAD software, with an energy consumption of 13.23 MJ/Kg of anhydrous ethanol. Finally, several ionic liquids were analyzed and are proposed as potential solvents for the recovery of bioethanol for the design of an integrated extraction–fermentation–separation process, according to their ability to extract ethanol from aqueous solutions and their biocompatibility with the microorganism used in this study.

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36

Zhao-Dong, Nan, Tan Zhi-Cheng, and Sun Li-Xian. "Thermodynamic Investigation of the Azeotrope of Water and Ethanol." Acta Physico-Chimica Sinica 20, no. 06 (2004): 626–30. http://dx.doi.org/10.3866/pku.whxb20040615.

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37

Artemenko, Sergey, Samir Haddad, and Victor Mazur. "Azeotrope breaking potential of ionic liquids in separation processes." Journal of Molecular Liquids 235 (June 2017): 49–52. http://dx.doi.org/10.1016/j.molliq.2016.12.006.

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38

Unterreiner, Janine M., Mark A. McHugh, and Val J. Krukonis. "Breaking the trimethyl borate-methanol azeotrope with supercritical methane." Industrial & Engineering Chemistry Research 30, no. 4 (April 1991): 740–45. http://dx.doi.org/10.1021/ie00052a018.

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39

Usol’tseva, O. O., L. A. Serafimov, and Yu A. Pisarenko. "Appearance of an internal tangential azeotrope in ternary systems." Theoretical Foundations of Chemical Engineering 44, no. 3 (June 2010): 293–99. http://dx.doi.org/10.1134/s0040579510030085.

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40

Frolkova, A. V., A. A. Akishina, and A. K. Frolkova. "Binodal varieties of the systems with four-component azeotrope." Theoretical Foundations of Chemical Engineering 50, no. 1 (January 2016): 110–18. http://dx.doi.org/10.1134/s004057951601005x.

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41

Forner, F., A. Klein, and J. U. Repke. "Trennung homogener Azeotrope mittels Zweidruckrektifikation - Eine Analyse des Betriebsverhaltens." Chemie Ingenieur Technik 77, no. 6 (June 2005): 763–71. http://dx.doi.org/10.1002/cite.200500024.

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42

Ribeiro, Filipe M. S., Carlos F. R. A. C. Lima, Artur M. S. Silva, and Luís M. N. B. F. Santos. "Experimental Evidence for Azeotrope Formation from Protic Ionic Liquids." ChemPhysChem 19, no. 18 (June 20, 2018): 2364–69. http://dx.doi.org/10.1002/cphc.201800335.

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43

de Melo, Jonas R. M., Lidia Tiggeman, Katia Rezzadori, Juliana Steffens, Marshall Palliga, J. Vladimir Oliveira, Marco Di Luccio, and Marcus V. Tres. "Desolventizing of soybean oil/azeotrope mixtures using ceramic membranes." Environmental Technology 38, no. 16 (October 13, 2016): 1969–79. http://dx.doi.org/10.1080/09593330.2016.1242658.

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44

Gomis, Vicente, Alicia Font, and Maria Dolores Saquete. "Homogeneity of the water+ethanol+toluene azeotrope at 101.3kPa." Fluid Phase Equilibria 266, no. 1-2 (April 2008): 8–13. http://dx.doi.org/10.1016/j.fluid.2008.01.018.

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45

Zhuang, Liwei, Qingyuan Cao, Fei Liang, Yichao Hu, Weite Su, Xin Wen, Xiao-Hua Ma, and Zhen-Liang Xu. "Exploring distillation-pervaporation hybrid process in a single column using hollow fiber pervaporation composite membranes as structured packing." Materials Express 10, no. 5 (May 1, 2020): 701–9. http://dx.doi.org/10.1166/mex.2020.1680.

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This study developed a novel strategy for azeotrope separation such as ethanol-water binary system. Distillation-pervaporation hybrid process was employed by using hollow fiber pervaporation composite membranes as structured packing in a single hybrid column rather than using pervaporation as an externally connected unit of the distillation column. The separating limitation of azeotrope challenged in conventional distillation could be readily overcome by continually removing water from the hybrid system via pervaporation. The competition between distillation and pervaporation has been found to be cause of unexpected concentration distribution in the hybrid column. The mass flux of mixture decreased with time whereas the selectivity of water to ethanol first increased then decreased with time. Analysis of this system illustrated that the increase in heating power and membrane area shortened time for obtaining certain content of ethanol in the mixture. However, faster decline in mass flux occurred due to an increase in the removal rate of water. With respect to its simplicity, efficiency and broad applicability, this hybrid process is expected to provide a benchmark for the enhancement of distillation-pervaporation process by hollow fiber membrane packing.

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Феофанова, Мариана Александровна, Юлия Ивановна Софронова, Андрей Николаевич Евдокимов, and Александр Вячеславович Курзин. "APPLICATION OF IMIDAZOLINES BASED ON TALL OIL FATTY ACIDS AND THEIR QUATERNARY SALTS FOR THE SEPARATION OF THE BINARY NON-AQUEOUS AZEOTROPE SYSTEMS." Вестник Тверского государственного университета. Серия: Химия, no. 4(42) (December 21, 2020): 63–69. http://dx.doi.org/10.26456/vtchem2020.4.7.

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Методом экстрактивной (в том числе солевой) ректификации с использованием имидазолинов и четвертичных солей на их основе разделены на компоненты неводные двойные азеотропные системы. В качестве разделяющих агентов выбраны: промышленный продукт 1-гидроксиэтил-2-алкенил-2-имидазолин на основе жирных кислот таллового масла, а также его четвертичные соли - хлорид и тетрафторборат 1-гидроксиэтил-2-алкенил-3-бензил-2-имидазолиния. Для разделения были использованы неводные азеотропные системы: ацетон-метанол, метилацетат-метанол, этилацетат-этанол и хлороформ-метанол. Равновесие жидкость-пар в соответствующих тройных системах исследовано в модифицированном приборе Отмера при 101,3 кПа, состав жидкой и паровой фаз определен газохроматографическим методом анализа. Минимальные концентрации (в мольных долях) имидазолина и имидазолиниевых солей для разрушения азеотропов составили 0,156-0,264. Для корреляции экспериментальных данных о парожидкостном равновесии в системах, содержащих имидазолиниевые соли использована электролитная модель NRTL. Средние абсолютные отклонения расчетных данных от экспериментальных значений мольного содержания растворителей в паровой фазе и температуры в системах составили 0,007-0,008 и 0,25-0,35 К, соответственно. The non-aqueous binary azeotrope systems have been separated into components by the method of extractive rectification (and salt rectification) using imidazolines and their quaternary salts. The following were selected as separating agents: industrial product 1-hydroxyethyl-2-alkenyl-2-imidazoline based on tall oil fatty acids, as well as its quaternary salts - chloride and tetrafluoroborate 1-hydroxyethyl-2-alkenyl-3-benzyl-2-imidazolinium. Non-aqueous azeotrope acetone - methanol, methyl acetate - methanol, ethyl acetate - ethanol, and chloroform - methanol systems were used for separation. The vapor-liquid equilibrium in the corresponding ternary systems was investigated in a modified Othmer still at 101.3 kPa, the composition of the liquid and vapor phases was determined by gas chromatographic analysis. The minimum concentrations (in molar fractions) of imidazoline and imidazolinium salts for the azeotrope breaking were 0.156-0.264. The mean absolute deviations between experimental and calculated data for the solvent mole fraction in the vapor phase and temperature in the imidazolinium salt containing systems were 0,007-0,008 and 0,25-0,35 К respectively.

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Hong, Jane H., and Riki Kobayashi. "To break an azeotrope. 1. The use of n-pentane to break the carbon dioxide-ethane azeotrope, for carbon dioxide EOR gas processing." Industrial & Engineering Chemistry Process Design and Development 25, no. 3 (July 1986): 736–41. http://dx.doi.org/10.1021/i200034a024.

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48

Andreatta, Alfonsina E., Matthew P. Charnley, and Joan F. Brennecke. "Using Ionic Liquids To Break the Ethanol–Ethyl Acetate Azeotrope." ACS Sustainable Chemistry & Engineering 3, no. 12 (November 17, 2015): 3435–44. http://dx.doi.org/10.1021/acssuschemeng.5b01175.

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Ramalingam, Anantharaj, Ramesh Kumar Gurunathan, and Pratheeba Chanda Nagarajan. "Investigation of Potential Azeotrope Breakers Using DFT and COSMO Approach." ACS Omega 5, no. 27 (June 26, 2020): 16885–900. http://dx.doi.org/10.1021/acsomega.0c02086.

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Wang, Yanhong, Chunmei Gong, Jinsheng Sun, Hong Gao, Shuai Zheng, and Shimin Xu. "Separation of ethanol/water azeotrope using compound starch-based adsorbents." Bioresource Technology 101, no. 15 (August 2010): 6170–76. http://dx.doi.org/10.1016/j.biortech.2010.02.102.

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