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Journal articles on the topic 'Non-azeotropic mixtures'

Author: Grafiati

Published: 9 March 2023

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1

MURATA, Keiji, and Kenichi HASHIZUME. "Forced convection boiling of non-azeotropic mixtures." Transactions of the Japan Society of Mechanical Engineers Series B 54, no. 506 (1988): 2856–63. http://dx.doi.org/10.1299/kikaib.54.2856.

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2

Camporese, R., G. Bigolaro, and A. Murasckin. "Interaction parameter, k12, for non-azeotropic refrigerant mixtures." International Journal of Refrigeration 8, no. 5 (September 1985): 270–74. http://dx.doi.org/10.1016/0140-7007(85)90005-2.

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3

Tóth, András József, and Szilvia Schmidt. "Method for Efficient Regeneration of Solvent Mixture: Extractive Heterogeneous-Azeotropic Distillation." Műszaki Tudományos Közlemények 15, no. 1 (October 1, 2021): 103–7. http://dx.doi.org/10.33894/mtk-2021.15.20.

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Abstract The fine chemical and pharmaceutical industries use large amounts of various organic solvents in their manufacturing processes. By reusing them, production costs can be significantly reduced. If we can regenerate waste solvent mixtures, we have the opportunity to reuse them in the production process or in other production processes. Our study illustrates an efficient regeneration process using the example of a four-component solvent mixture. Calculations were performed in a professional process simulator to demonstrate that the highly non-ideal Water-Ethyl Alcohol-Methyl Ethyl Ketone-Ethyl Acetate solvent mixture can be efficiently decomposed into azeotropic pairs and thus regenerated by the extractive heterogeneous-azeotropic distillation technique.

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4

Deng, Han, Maria Fernandino, and Carlos A. Dorao. "A numerical investigation of flow boiling of non-azeotropic and near-azeotropic binary mixtures." International Journal of Refrigeration 49 (January 2015): 99–109. http://dx.doi.org/10.1016/j.ijrefrig.2014.10.003.

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5

Mezentseva, N. N., V. A. Mukhin, and I. V. Mezentsev. "Heat transfer at nucleate boiling of non-azeotropic mixtures." Journal of Physics: Conference Series 891 (November 10, 2017): 012034. http://dx.doi.org/10.1088/1742-6596/891/1/012034.

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6

Azzolin, M., A. Berto, S. Bortolin, and D. Del Col. "Heat transfer degradation during condensation of non-azeotropic mixtures." Journal of Physics: Conference Series 923 (November 2017): 012017. http://dx.doi.org/10.1088/1742-6596/923/1/012017.

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7

Xu, Chen, Zuoqin Qian, and Jie Ren. "A Comprehensive Experimental Investigation of Additives to Enhance Pool Boiling Heat Transfer of a Non-Azeotropic Mixture." Entropy 24, no. 11 (October 26, 2022): 1534. http://dx.doi.org/10.3390/e24111534.

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Adding nanoparticles or surfactants to pure working fluid is a common and effective method to improve the heat transfer performance of pool boiling. The objective of this research is to determine whether additives have the same efficient impact on heat transfer enhancement of the non-azeotropic mixture. In this paper, Ethylene Glycol/Deionized Water (EG/DW) was selected as the representing non-azeotropic mixture, and a comparative experiment was carried out between it and the pure working fluid. In addition, the effects of different concentrations of additives on the pool boiling heat transfer performance under different heat fluxes were experimentally studied, including TiO2 nanoparticles with different particle diameters, different kinds of surfactants, and mixtures of nanofluids and surfactants. The experimental results showed that the nanoparticles deteriorated the heat transfer of the EG/DW solution, while the surfactant enhanced the heat transfer of the solution when the concentration closed to a critical mass fraction (CMC). However, the improvement effect was unsteady with the increase in the heat flux density. The experimental results suggest that the mass transfer resistance of the non-azeotropic mixture is the most important factor in affecting heat transfer enhancement. Solutions with 20 nm TiO2 obtained a steady optimum heat transfer improvement by adding surfactants.

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8

Zhukov, V. E., N. N. Mezentseva, and I. V. Mezentsev. "Vaporization in non-azeotropic and azeotropic alcohol-water mixtures at a flow in a heated circular channel." Thermophysics and Aeromechanics 28, no. 5 (September 2021): 757–60. http://dx.doi.org/10.1134/s0869864321050188.

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9

Davletbaeva, Ilsiya M., Alexander V. Klinov, Alina R. Khairullina, Alexander V. Malygin, and Nikolay V. Madaminov. "Vapor–Liquid Equilibrium in Binary and Ternary Azeotropic Solutions Acetonitrile-Ethanol-Water with the Addition of Amino Esters of Boric Acid." Processes 10, no. 10 (October 19, 2022): 2125. http://dx.doi.org/10.3390/pr10102125.

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The effect of amino esters of boric acid (AEBA) on the conditions of vapor–liquid equilibrium in binary mixtures of acetonitrile–water, ethanol–acetonitrile and a three-component mixture of ethanol-acetonitrile-water was investigated. Residual curves and vapor–liquid phase equilibrium conditions (TPXY data) were experimentally measured at atmospheric pressure for a binary mixture of acetonitrile-AEBA and a triple mixture of acetonitrile-water-AEBA. Previously unknown energy binary parameters of groups B, CH2N with group CH3CN were determined for the UNIFAC model. The correction of the value of the binary parameter water—acetonitrile was carried out. On the basis of thermodynamic modeling, the degree of influence of AEBA on the relative volatility of acetonitrile in binary and ternary mixtures was analyzed. It is shown that the use of AEBA removes all azeotropic points in the studied mixtures. In this case, acetonitrile turns out to be a volatile component, and water is a non-volatile component in the entire concentration range.

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10

Andras, Csaba Dezso, Eva Molnos, Laszlo Matyas, and Alexandru Szep. "New Fitting Method for Vapour-Liquid Equilibrium Data and its Application for Ethanol-Water Distillation Process Modeling." Revista de Chimie 71, no. 7 (August 4, 2020): 114–25. http://dx.doi.org/10.37358/rc.20.7.8219.

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For modeling and simulation of distillation processes, the main information required is the vapour-liquid equilibrium (VLE) data. These are available as discrete values, but for modeling purpose, an analytical function would be more suitable. We developed a simple calculation protocol to obtain a single continuous function for the VLE curve on the entire concentration domain, without using thermodynamic functions. The fitting parameters of binary ethanol-water mixture VLE curve were determined. The methodology is suitable for fitting continuous functions on VLE data of any binary or multicomponent, non-ideal (even azeotropic) mixtures.

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11

Toth, Andras Jozsef, Agnes Szanyi, Katalin Koczka, and Peter Mizsey. "Enhanced separation of highly non-ideal mixtures with extractive heterogeneous-azeotropic distillation." Separation Science and Technology 51, no. 7 (November 3, 2015): 1238–47. http://dx.doi.org/10.1080/01496395.2015.1107099.

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12

Mezentseva, N. N. "Efficiency of vapor compression heat pumps based on non-azeotropic refrigerant mixtures." Thermophysics and Aeromechanics 18, no. 2 (June 2011): 323–30. http://dx.doi.org/10.1134/s0869864311020120.

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13

Kubota, Hironobu, Takahiro Ikawa, Yoshiyuki Tanaka, Tadashi Makita, and Kiyotada Miyoshi. "Vapor-liquid equilibria of non-azeotropic halogenated hydrocarbon mixtures under high pressure." JOURNAL OF CHEMICAL ENGINEERING OF JAPAN 23, no. 2 (1990): 155–59. http://dx.doi.org/10.1252/jcej.23.155.

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14

Sami, S. M., and W. LeBlanc. "Study of non-azeotropic refrigerant mixtures behaviour in gravity assisted heat pipes." Heat Recovery Systems and CHP 11, no. 5 (January 1991): 393–405. http://dx.doi.org/10.1016/0890-4332(91)90007-q.

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15

Nahra, Ziad, and Erling Næss. "Heat transfer in pool boiling of binary and ternary non-azeotropic mixtures." Heat and Mass Transfer 45, no. 7 (June 23, 2007): 951–58. http://dx.doi.org/10.1007/s00231-007-0294-z.

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16

Chavan, Akshaya Ravindra, and Sunil S. Bhagwat. "Synergistic behavior of SLS-OPE-10 binary mixtures at their CMC." Tenside Surfactants Detergents 59, no. 2 (February 28, 2022): 134–43. http://dx.doi.org/10.1515/tsd-2021-2398.

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Abstract The micellation behaviour of mixtures of sodium lauryl sulphate (SLS) and octylphenol ethoxylate-10 (OPE-10) was investigated using tensiometry and dye solubilisation. The interaction parameters for the system were determined using Rubingh’s model for non-ideality and the adsorption parameters were calculated. The surfactant mixture was found to behave synergistically in terms of CMC reduction and dye solubilisation. Furthermore, the mixture appears to mimic the adsorption and micellation properties of OPE-10 more closely than SLS, regardless of composition. With this knowledge, and considering that OPE-10 is typically more expensive than SLS, the formulator can now use only a fraction of the required amount of OPE-10 for a given application (instead of using 100% OPE-10), resulting in high performance yet economical products. It was also found that the said mixture exhibits azeotropic behaviour at a certain fixed composition.

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17

Högberg, Marine, and Thore Berntsson. "Non-azeotropic mixtures as working fluids in two-stage economizer-type heat pumps." International Journal of Refrigeration 17, no. 6 (July 1994): 417–29. http://dx.doi.org/10.1016/0140-7007(94)90077-9.

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18

Sami, S. M., P. Tulej, and L. Fang. "Heat transfer in forced convection boiling of oil–non-azeotropic binary refrigerant mixtures." International Journal of Energy Research 17, no. 9 (December 1993): 905–13. http://dx.doi.org/10.1002/er.4440170910.

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19

Sami, S. M., and Y. Zhou. "Numerical prediction of heat pump dynamic behaviour using ternary non-azeotropic refrigerant mixtures." International Journal of Energy Research 19, no. 1 (January 1995): 19–35. http://dx.doi.org/10.1002/er.4440190105.

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20

YOSHIDA, Suguru, Takashi MATSUNAGA, Hideo MORI, and Katsumi OHISHI. "Heat transfer to non-azeotropic mixtures of refrigerants flowing in a horizontal evaporator tube." Transactions of the Japan Society of Mechanical Engineers Series B 56, no. 524 (1990): 1084–89. http://dx.doi.org/10.1299/kikaib.56.1084.

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21

Mezentseva, N. N., I. V. Mezentsev, and A. V. Meleshkin. "Nucleate boiling at the forced flow of binary non-azeotropic mixtures in horizontal tubes." MATEC Web of Conferences 23 (2015): 01027. http://dx.doi.org/10.1051/matecconf/20152301027.

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22

Wasylkiewicz, S. K. "Design of heterogeneous distillation columns for separation of azeotropic non-reactive and reactive mixtures." Computers & Chemical Engineering 23 (June 1999): S125—S128. http://dx.doi.org/10.1016/s0098-1354(99)80032-5.

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23

Sami, S. M., and J. Schnotale. "Prediction of forced convective condensation of non-azeotropic refrigerant mixtures inside enhanced surface tubing." Applied Scientific Research 50, no. 2 (March 1993): 149–68. http://dx.doi.org/10.1007/bf00849550.

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24

Chu-Jun, Gu, and Lin Lan. "A heat-power cycle for electricity generation from hot water with non-azeotropic mixtures." Energy 13, no. 6 (June 1988): 529–36. http://dx.doi.org/10.1016/0360-5442(88)90006-0.

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25

Sami, S. M., and M. A. Comeau. "Experimental study of the dynamic behaviour of non-azeotropic binary mixtures in heat pumps." Heat Recovery Systems and CHP 11, no. 6 (January 1991): 505–15. http://dx.doi.org/10.1016/0890-4332(91)90052-6.

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26

Tóth, András József, Ágnes Szanyi, Enikő Haaz, and Péter Mizsey. "Separation of Process Wastewater with Extractive Heterogeneous-Azeotropic Distillation." Hungarian Journal of Industry and Chemistry 44, no. 1 (October 1, 2016): 29–32. http://dx.doi.org/10.1515/hjic-2016-0003.

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Abstract The application of vapour-liquid equilibria-based separation alternatives can be extraordinarily complicated for the treatment of process wastewaters containing heterogeneous-azeotropic. Despite dissimilar successfully tested methods for separation, there is possibility to get better distillation method by enabling the separation of more and more specific process wastewater. Extractive heterogeneous-azeotropic distillation (EHAD) is a new advance in treatment of fine chemical wastewater showing special features to cope with the treatment of highly non-ideal mixtures. This method combines the worth of heterogeneous-azeotropic and extractive distillations in one apparatus without addition of any extra materials. The study of the separations of ternary component process wastewater from the fine chemical industry shows both in the modelled and experimental results that EHAD can be successfully applied. The measured and modelled compositions at extreme purities, that is, close to 0% or 100%, can be different because of the inaccuracies of the modelling. This highlights the paramount importance of the experiments if special extra-fine chemicals with almost no impurities, e.g. of pharmacopoeial quality are to be produced by special distillation technique. This study expands the application of EHAD technique, this new field is the separation of process wastewaters.

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27

Mastrullo, R., A. W. Mauro, G. Napoli, F. Pelella, and L. Viscito. "Flow boiling of azeotropic and non-azeotropic mixtures. Effect of the glide temperature difference on the nucleate boiling contribution: assessment of methods." Journal of Physics: Conference Series 1599 (August 2020): 012053. http://dx.doi.org/10.1088/1742-6596/1599/1/012053.

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28

Krishnaiah, Duduku, Rosalam Sarbatly, S. M. Anisuzzama, Rajesh Nithyanand, and Phong Ming San. "Effect of Ultrasound on Liquid Phase Adsorption of Azeotropic and Non-azeotropic Mixtures: Generation of Adsorption Isotherms According to Gibbs Dividing Plane Theory." Journal of Applied Sciences 14, no. 13 (June 15, 2014): 1420–24. http://dx.doi.org/10.3923/jas.2014.1420.1424.

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29

Gong, M. Q., E. C. Luo, J. F. Wu, and Y. Zhou. "On the temperature distribution in the counter flow heat exchanger with multicomponent non-azeotropic mixtures." Cryogenics 42, no. 12 (December 2002): 795–804. http://dx.doi.org/10.1016/s0011-2275(02)00148-0.

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30

Shao, D. W., and E. Granryd. "Experimental and theoretical study on flow condensation with non-azeotropic refrigerant mixtures of R32/R134a." International Journal of Refrigeration 21, no. 3 (May 1998): 230–46. http://dx.doi.org/10.1016/s0140-7007(98)00015-2.

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31

Barroso-Maldonado, J. M., J. A. Montañez-Barrera, J. M. Belman-Flores, and S. M. Aceves. "ANN-based correlation for frictional pressure drop of non-azeotropic mixtures during cryogenic forced boiling." Applied Thermal Engineering 149 (February 2019): 492–501. http://dx.doi.org/10.1016/j.applthermaleng.2018.12.082.

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32

Zhang, Shengjun, Huaixin Wang, and Tao Guo. "Experimental investigation of moderately high temperature water source heat pump with non-azeotropic refrigerant mixtures." Applied Energy 87, no. 5 (May 2010): 1554–61. http://dx.doi.org/10.1016/j.apenergy.2009.11.001.

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33

Shamirzaev, A. S., and V. V. Kuznetsov. "An experimental study of flow condensation with non-azeotropic refrigerant mixtures of R32/R134a in microchannels." Journal of Physics: Conference Series 1677 (November 2020): 012095. http://dx.doi.org/10.1088/1742-6596/1677/1/012095.

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34

Haaz, Eniko, Botond Szilagyi, Daniel Fozer, and Andras Jozsef Toth. "Combining extractive heterogeneous-azeotropic distillation and hydrophilic pervaporation for enhanced separation of non-ideal ternary mixtures." Frontiers of Chemical Science and Engineering 14, no. 5 (March 6, 2020): 913–27. http://dx.doi.org/10.1007/s11705-019-1877-1.

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35

Itard, L. C. M. "Wet compression versus dry compression in heat pumps working with pure refrigerants or non-azeotropic mixtures." International Journal of Refrigeration 18, no. 7 (September 1995): 495–504. http://dx.doi.org/10.1016/0140-7007(95)93788-l.

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36

Mezentseva, N. N., and I. V. Mezentsev. "Peculiarities of determination of the heat transfer coefficient at boiling of non-azeotropic mixtures in tubes." Journal of Physics: Conference Series 1105 (November 2018): 012047. http://dx.doi.org/10.1088/1742-6596/1105/1/012047.

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37

Miyara, Akio, Shigeru Koyama, and Tetsu Fujii. "Consideration of the performance of a vapour-compression heat-pump cycle using non-azeotropic refrigerant mixtures." International Journal of Refrigeration 15, no. 1 (January 1992): 35–40. http://dx.doi.org/10.1016/0140-7007(92)90065-3.

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38

Zhang, Xiaoyan, Changfa Ji, and Xiuling Yuan. "Prediction method for evaporation heat transfer of non-azeotropic refrigerant mixtures flowing inside internally grooved tubes." Applied Thermal Engineering 28, no. 14-15 (October 2008): 1974–83. http://dx.doi.org/10.1016/j.applthermaleng.2007.12.009.

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39

Benyounes, Hassiba, Khadidja Benyahia, Weifeng Shen, Vincent Gerbaud, Lichun Dong, and Shun’an Wei. "Novel Procedure for Assessment of Feasible Design Parameters of Dividing-Wall Columns: Application to Non-azeotropic Mixtures." Industrial & Engineering Chemistry Research 54, no. 19 (May 6, 2015): 5307–18. http://dx.doi.org/10.1021/ie5048576.

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40

Yu, Jiawen, Xiaojun Li, Yi Li, and Yue Wang. "Study on calculation method of condensation heat transfer for non-azeotropic hydrocarbon mixtures in helically coiled tubes." Journal of Thermal Analysis and Calorimetry 141, no. 1 (December 11, 2019): 177–86. http://dx.doi.org/10.1007/s10973-019-09150-3.

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41

Sami, S. M., P. J. Tulej, and B. Song. "Forced convective condensation and boiling of ternary non-azeotropic refrigerant mixtures inside water/refrigerant enhanced surface tubing." International Journal of Energy Research 18, no. 8 (November 1994): 751–64. http://dx.doi.org/10.1002/er.4440180806.

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42

Fan, Xiao-Wei, Fu-Jun Ju, Xian-Ping Zhang, and Fang Wang. "Thermodynamic comparision of R744/R600a and R744/R600 used in mid-high temperature heat pump system." Thermal Science 18, no. 5 (2014): 1655–59. http://dx.doi.org/10.2298/tsci1405655f.

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The mid-high temperature heat pump provides hot water at a relatively high temperature using some industrial waste heat as its source. Now, the main refrigerants in this application are CFC114, HCFC123, and HCFC142b, etc., which are scheduled to be phased out due to their high ozone depletion potential and global warmth potential. Some studies have been conducted to find an eco-friendly alternative. In this paper, the natural non-azeotropic mixtures R744/R600a and R744/R600 are analyzed as alternatives. The performance of the heat pump system using new mixture is discussed and compared with those with CFC114, HCFC123, and HCFC142b. Under the given operating conditions, the maximum heating COP should occur at the mass fractions of 18/82 for R744/R600a and 10/90 for R744/R600. Both of their COP are higher than those with the refrigerants of CFC114, HCFC123, and HCFC142b. The COP and volumetric heating capacity of the system with R744/R600a are superior to those with R744/R600.

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43

Bukin, Vladimir Grigorievich, Alexey Vasilievich Ezhov, and Aleksander Ivanovich Andreev. "Temperature-entropy diagrams for calculating cycles of refrigerating machines using refrigerant mixtures." Vestnik of Astrakhan State Technical University. Series: Marine engineering and technologies 2020, no. 4 (November 18, 2020): 79–86. http://dx.doi.org/10.24143/2073-1574-2020-4-79-86.

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The article represents the advantages and disadvantages of refrigeration machines operating on non-azeotropic refrigerant mixtures. There has been illustrated their specific feature in comparison with pure substances: they are non-isothermal during phase transitions. It can be effective when cooling or heating flows that significantly change the temperature, and ineffective when working with volumes, where it is necessary to maintain a constant temperature. In the first case there takes place a decrease in the internal irreversibility of heat transfer processes in evaporators and condensers; in the second case - an increase. When using mixed refrigerants, it is possible to simultaneously obtain several temperature levels in a single-stage machine at the same pressure in the evaporators, they can obtain low boiling points of the refrigerant without vacuum in the evaporator and regulate the refrigeration capacity of the machine by changing the composition of the mixture. The prospects of using mixtures of working bodies of refrigerating machines have been proved. The diagrams T-S, T-ξ, i-ξ are presented allowing to calculate the cycle of the machine, to determine its operating parameters and to calculate the technical and energy characteristics. The developed thermal diagrams make it possible to accurately examine the dynamics of the boiling and condensation processes of a binary mixture, show the change in the concentration of the mixture in the vapor and liquid phases and make it possible to construct and calculate the cycle of a refrigeration machine operating on a mixed refrigerant. Examples of constructing cycles of two schemes of refrigeration machines operating on a mixed refrigerant are considered: with separation of the working substance flow and without separation. Methods for calculating the cycle are provided

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44

Gu, Yujiong, and Zhi Geng. "Comprehensive evaluation of supercritical power cycle system using non-azeotropic mixtures driven by medium-temperature solar heat source." Journal of Renewable and Sustainable Energy 10, no. 6 (November 2018): 064706. http://dx.doi.org/10.1063/1.5047544.

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45

Zhang, ShengJun, HuaiXin Wang, and Tao Guo. "Evaluation of non-azeotropic mixtures containing HFOs as potential refrigerants in refrigeration and high-temperature heat pump systems." Science China Technological Sciences 53, no. 7 (July 2010): 1855–61. http://dx.doi.org/10.1007/s11431-010-4008-2.

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46

Arcasi, A., R. Mastrullo, A. W. Mauro, and L. Viscito. "Adiabatic frictional pressure gradient during flow boiling of pure refrigerant R1233zd and non-azeotropic mixtures R448A, R452A and R455A." Journal of Physics: Conference Series 2177, no. 1 (April 1, 2022): 012045. http://dx.doi.org/10.1088/1742-6596/2177/1/012045.

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Abstract The research on two-phase flow characteristics of refrigerants is of primary importance in several fields, such as air conditioning and refrigeration systems. Therefore, the determination of the pressure drop during flow boiling is important for the correct design of evaporators and heat spreaders systems. This paper presents a collection of experiments on flow boiling pressure drop using pure refrigerant R1233zd and new low-GWP refrigerant mixtures R448A, R452A and R455A. All tests were performed in adiabatic conditions, in a smooth horizontal stainless-steel tube having an internal diameter of 6.0 mm and a thickness of 1.0 mm. The effect of operating parameters, such as (bubble) saturation temperature (from 25 to 65 °C) and mass flux (from 150 to 600 kg/m2s) is investigated and discussed, and the performance of the chosen fluids is also compared. Finally, an assessment of existing prediction methods is carried-out to find the most suitable correlations for two-phase pressure drop evaluation.

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47

Del Col, Davide, Marco Azzolin, Stefano Bortolin, and Claudio Zilio. "Two-phase pressure drop and condensation heat transfer of R32/R1234ze(E) non-azeotropic mixtures inside a single microchannel." Science and Technology for the Built Environment 21, no. 5 (June 29, 2015): 595–606. http://dx.doi.org/10.1080/23744731.2015.1047718.

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48

Chiou, C. B., D. C. Lu, C. Y. Liao, and Y. Y. Su. "Experimental study of forced convective boiling for non-azeotropic refrigerant mixtures R-22/R-124 in horizontal smooth tube." Applied Thermal Engineering 29, no. 8-9 (June 2009): 1864–71. http://dx.doi.org/10.1016/j.applthermaleng.2008.09.004.

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49

Zhang, Lili, Guanmin Zhang, Yi Zhang, Maocheng Tian, and Jingzhi Zhang. "A 2D numerical study on the condensation characteristics of three non-azeotropic binary hydrocarbon vapor mixtures on a vertical plate." Chinese Journal of Chemical Engineering 28, no. 11 (November 2020): 2746–57. http://dx.doi.org/10.1016/j.cjche.2020.07.001.

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50

Raeva, V. M., and A. M. Dubrovsky. "Comparison of extractive distillation flowsheets for methanol–tetrahydrofuran–water mixtures." Fine Chemical Technologies 15, no. 3 (July 7, 2020): 21–30. http://dx.doi.org/10.32362/2410-6593-2020-15-3-21-30.

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Abstract:

Objectives. Synthesis and comparative analysis of the extractive distillation flowsheets for aqueous mixtures of solvents utilized in pharmaceutical industries using the example of a methanol−tetrahydrofuran−water system with various compositions. The ternary system contains two minimally boiling azeotropes that exist in a vapor–liquid phase equilibrium. To evaluate the selective effect of glycerol, the phase equilibria of the methanol–tetrahydrofuran–water and methanol–tetrahydrofuran–water–glycerol systems at 101.32 kPa were studied.Methods. The calculations were carried out in the Aspen Plus V.9.0 software package. The vapor–liquid equilibria were simulated using the non-random two-liquid (NRTL) equation with the binary interaction parameters of the software package database. To account for the non-ideal behavior of the vapor phase, the Redlich–Kwong equation of state was used. The calculations of the extractive distillation schemes were carried out at 101.32 kPa.Results. The conceptual flowsheets of extractive distillation are proposed. The flowsheets consist of three (schemes I–III) or four (scheme IV) distillation columns operating at atmospheric pressure. In schemes I and II, the extractive distillation of the mixtures is carried out with tetrahydrofuran isolation occurring in the distillate stream. Further separation in the schemes differs in the order of glycerol isolation: in the third column for scheme I (traditional extractive distillation complex) or in the second column for scheme II (two-column extractive distillation complex + methanol/water separation column). Sсheme III caters to the complete dehydration of the basic ternary mixtures, followed by the extractive distillation of the azeotropic methanol–tetrahydrofuran system, also with glycerol. Sсheme IV includes a preconcentration column (for the partial removal of water) and a traditional extractive distillation complex.Conclusions. According to the criterion of least energy consumption for separation (the total load of the reboilers of distillation columns), sсheme I (a traditional complex of extractive distillation) is recommended. Additionally, the energy expended for the separation of the basic equimolar mixture using glycerol as the extractive agent was compared with that expended using another selective agent: 1,2-ethanediol. Glycerol is an effective extractive agent because it reduces energy consumption, in comparison with 1,2-ethanediol, by more than 5%.

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