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Journal articles on the topic 'Azeotropes'

Author: Grafiati

Published: 4 June 2021

Last updated: 27 July 2024

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1

Taipabu, Muhammad Ikhsan, Wei Wu, Karthickeyan Viswanathana, Nikmans Hattu, Ervina Rumpakwakra, and Micky Kololu. "SEPARATION OF ETHANOL-WATER AZEOTROPE MIXTURES USING EXTRACTIVE DISTILLATION METHOD." ALE Proceeding 6 (November 1, 2023): 198–203. http://dx.doi.org/10.30598/ale.6.2023.198-203.

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Extractive distillation is a specialized distillation process that involves adding an additional component (extractive agent or solvent/entrainer) to the mixture in order to alter the relative volatilities of the components and enable their separation, even when they form azeotropes. This technique is commonly used to separate azeotropic mixtures, such as ethanol-water azeotropes. The ethanol-water azeotrope is a well-known example, where the mixture contains around 95.6 wt% ethanol and 4.4 wt% water. Traditional distillation methods cannot separate these components efficiently due to the azeotropic behavior. However, extractive distillation offers a solution by introducing a third component (entrainer) that forms a ternary azeotrope, which has different properties compared to the binary azeotrope (ethanol-water). This study presents the effect of the operating parameters (e.g., column configuration, pressure, entrainer type) on energy consumption while the purity of ethanol is set to 99.5 wt%. Appropriate entrainers (i.e., glycerol, ethylene glycol) are chosen to extract water from methanol at different compositions. The optimum design of ethanol-water azeotrope separation is obtained by using sensitivity analysis in Aspen Plus simulation. The results indicate the trade-off between solvent and reboiler duty consumption. An advanced comparison study is recommended, including the mixing of both solvents as entrainer.

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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

Hu, Xianbing, Lingjie Sun, Chengyang Yuan, Man Li, Hongsheng Dong, Lunxiang Zhang, Lei Yang, Jiafei Zhao, and Yongchen Song. "Principle and Feasibility Study of Proposed Hydrate-Based Cyclopentane Purification Technology." Energies 16, no. 12 (June 13, 2023): 4681. http://dx.doi.org/10.3390/en16124681.

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The separation of azeotropic mixtures has conventionally been one of the most challenging tasks in industrial processes due to the fact that components in the mixture will undergo gas–liquid phase transition at the same time. We proposed a method for separating azeotropes using hydrate formation as a solid–liquid phase transition. The feasibility of hydrate-based separation is determined by analyzing the crystal structure and chemical bonds of hydrate. Taking the azeotrope cyclopentane and neohexane in petroleum as an example, cyclopentane (95%) was purified to 98.56% yield using the proposed hydrate-based cyclopentane purification technology. However, this is difficult to achieve using conventional distillation methods. The proposed method is simple in operation and yields a good separation effect. This study provides a new method for separating cyclopentane and neohexane.

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6

Villalta-Cerdas, Adrian, Gregory D. Smith, Megan Carrison DeSmit, and John V. Goodpaster. "Room Temperature Evaporation Behavior of Homogeneous Azeotropes Used in Art Conservation Cleaning Treatments." Applied Sciences 13, no. 21 (November 2, 2023): 11962. http://dx.doi.org/10.3390/app132111962.

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Cleaning painted surfaces of their grime, aged varnishes, and discolored overpaint is one of the most common interventive treatments for art conservators. Carefully concocted solvent mixtures navigate the solubility differences between the material removed and the original paint underneath. However, these solutions may be altered by differential evaporation rates of the component solvents (zeotropic behavior), potentially leading to ineffectively weak cleaning or conversely overly strong residual liquid capable of damaging the underlying paint. Azeotropic solvent blends, which maintain a constant composition during evaporation, offer a promising solution. These blends consist of two or more solvents combined at precise concentrations to function as a single solvent. Additionally, pressure-maximum azeotropes feature higher vapor pressure compared to other mixtures, further minimizing contact time and sorption of the solvents into artworks. This study examines azeotropes of isopropanol with n-hexane and 2-butanone in cyclohexane, which have been used previously in art conservation. The evaporation behavior at room temperature of these boiling point azeotropes was assessed using vapor pressure measurements, refractive index determinations, gravimetric analysis, and gas chromatography. Results showed changes in composition during evaporation and found that the actual room temperature azeotropic composition can vary between 1 and 10% v/v in concentration with those commonly reported at their boiling points. Art conservators should be cautious when using azeotropic blends reported at boiling points significantly higher than room temperature. To ensure the safety and efficacy of these mixtures, it is recommended to determine individual azeotropic cleaning blends experimentally before their use.

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7

Kameshkov, Alexey V., Alexander A. Gaile, Vasily N. Klementyev, and Sofya D. Usanova. "FORMATION OF AZEOTROPIC MIXTURES OF N-METHYLPYRROLIDONE WITH HYDROCARBONS." Bulletin of the Saint Petersburg State Institute of Technology (Technical University) 56 (2021): 12–16. http://dx.doi.org/10.36807/1998-9849-2020-56-82-12-16.

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Using the limiting activity coefficients of the components of binary systems of N-methylpyrrolidone with n-alkanes and the conditions for the formation of azeotropes, it is found that N-methylpyrrolidone forms azeotropic mixtures with n-alkanes С9 - С 15, with alkylbenzenes С 10 - С 12 and with naphthalene. The formation of azeotropes with saturated hydrocarbons with a boiling point of 230-270 ° C must be taken into account when developing a technological scheme for the N-methylpyrrolidone regeneration unit, and also not to use this extractant for extraction purification of raw materials with a boiling point below 230 ° C

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8

Schlünder, E. U. "Azeotropes and pseudo-azeotropes." Fluid Phase Equilibria 51 (November 1989): 71–85. http://dx.doi.org/10.1016/0378-3812(89)80355-3.

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9

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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10

Maranas, C. D., C. M. McDonald, S. T. Harding, and C. A. Floudas. "Locating all azeotropes in homogeneous azeotropic systems." Computers & Chemical Engineering 20 (January 1996): S413—S418. http://dx.doi.org/10.1016/0098-1354(96)00079-8.

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11

Sutijan, Sutijan, Megan Jobson, and Robin Smith. "Synthesis of Ternary Homogeneous Azeotropic Distillation Sequences: Entrainer Selection." ASEAN Journal of Chemical Engineering 12, no. 1 (August 6, 2012): 20. http://dx.doi.org/10.22146/ajche.49752.

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This paper presents a methodology for automatic selection of entrainers for separating binary azeotropic mixtures using homogeneous azeotropic distillation. A new classification system for ternary mixtures based on the termini of distillation boundaries and the type (stability) of products and azeotropes is proposed. The new characterisation system is able to link candidate entrainers to flowsheet structures which can facilitate the separation. Existing entrainer selection criteria are extended to accommodate other promising entrainers, including light, intermediate and heavy-boiling entrainers.

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12

Schastnyy, Y. O., N. A. Romanova, and R. R. Gizatullin. "Evaluation of the possibility of separating commercial phenol from the phenolic fraction of coal tar." E3S Web of Conferences 266 (2021): 02011. http://dx.doi.org/10.1051/e3sconf/202126602011.

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This article is about the possibility of concentrating commercial coal phenol with a concentration of 99% by the weight method of rectification from the phenolic fraction of coal tar. The sufficiency of phenol is ensured by the kumol method, however, the consumption of phenol increases. Modeling of the vapor-liquid equilibrium of double and triple mixtures of components using the NRTL model showed the presence of the following positive homogeneous azeotropic mixtures: phenol-indane, phenol-indene. Modeling of the vapor-liquid equilibrium of double and triple mixtures of components using the NRTL model showed the presence of the following positive homogeneous azeotropic mixtures: phenol-indane, phenol-indene. The compositions and temperatures of these azeotropes are determined. The authors propose the isolation of phenol from the fraction and its purification from indane and indene by a clear rectification method. The technological scheme consisting of four devices is based on the analysis of the component composition of the initial mixture and the existing azeotropes. Modeling of the technological scheme showed that this scheme provides the release of phenol by 99% of the mass, which meets the requirements for coal phenol. After optimizing the technological parameters of the distillation columns, the estimated extraction costs will amount to 5.64 Gcal per ton of commercial phenol.

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13

Zheng, Yan-Zhen, Rui Zhao, Yu-Cang Zhang, and Yu Zhou. "A FTIR and DFT Combination Study to Reveal the Mechanism of Eliminating the Azeotropy in Ethyl Propionate–n-Propanol System with Ionic Liquid Entrainer." International Journal of Molecular Sciences 24, no. 13 (June 25, 2023): 10597. http://dx.doi.org/10.3390/ijms241310597.

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Ionic liquids (ILs) have presented excellent behaviors in the separation of azeotropes in extractive distillation. However, the intrinsic molecular nature of ILs in the separation of azeotropic systems is not clear. In this paper, Fourier-transform infrared spectroscopy (FTIR) and theoretical calculations were applied to screen the microstructures of ethyl propionate–n-propanol–1-ethyl-3-methylimidzolium acetate ([EMIM][OAC]) systems before and after azeotropy breaking. A detailed vibrational analysis was carried out on the v(C=O) region of ethyl propionate and v(O–D) region of n-propanol-d1. Different species, including multiple sizes of propanol and ethyl propionate self-aggregators, ethyl propionate–n-propanol interaction complexes, and different IL–n-propanol interaction complexes, were identified using excess spectroscopy and confirmed with theoretical calculations. Their changes in relative amounts were also observed. The hydrogen bond between n-propanol and ethyl propionate/[EMIM][OAC] was detected, and the interaction properties were also revealed. Overall, the intrinsic molecular nature of the azeotropy breaking was clear. First, the interactions between [EMIM][OAC] and n-propanol were stronger than those between [EMIM][OAC] and ethyl propionate, which influenced the relative volatilities of the two components in the system. Second, the interactions between n-propanol and [EMIM][OAC] were stronger than those between n-propanol and ethyl propionate. Hence, adding [EMIM][OAC] could break apart the ethyl propionate–n-propanol complex (causing the azeotropy in the studied system). When x([EMIM][OAC]) was lower than 0.04, the azeotropy still existed mainly because the low IL could not destroy the whole ethyl propionate–n-propanol interaction complex. At x(IL) > 0.04, the whole ethyl propionate–n-propanol complex was destroyed, and the azeotropy disappeared.

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14

Shephard, J. J., S. K. Callear, S. Imberti, J. S. O. Evans, and C. G. Salzmann. "Microstructures of negative and positive azeotropes." Physical Chemistry Chemical Physics 18, no. 28 (2016): 19227–35. http://dx.doi.org/10.1039/c6cp02450e.

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Azeotropes famously impose fundamental restrictions on distillation processes, yet their special thermodynamic properties make them highly desirable for a diverse range of industrial and technological applications. Using neutron diffraction, this study provides first insights into the microstructures of azeotropes.

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15

Ham, George E. "Terpolymer Relationships and Azeotropes." Journal of Macromolecular Science: Part A - Chemistry 28, no. 8 (August 1991): 733–42. http://dx.doi.org/10.1080/00222339108054053.

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16

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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17

Maier, Robert W., Joan F. Brennecke, and Mark A. Stadtherr. "Reliable computation of reactive azeotropes." Computers & Chemical Engineering 24, no. 8 (September 2000): 1851–58. http://dx.doi.org/10.1016/s0098-1354(00)00564-0.

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18

Shulgin, I., K. Fischer, O. Noll, and J. Gmehling. "Classification of Homogeneous Binary Azeotropes." Industrial & Engineering Chemistry Research 40, no. 12 (June 2001): 2742–47. http://dx.doi.org/10.1021/ie990897c.

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19

Wasylkiewicz, Stanislaw K., Leo C. Kobylka, and Francisco J. L. Castillo. "Pressure Sensitivity Analysis of Azeotropes." Industrial & Engineering Chemistry Research 42, no. 1 (January 2003): 207–13. http://dx.doi.org/10.1021/ie020079b.

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20

Fidkowski, Z. T., M. F. Malone, and M. F. Doherty. "Computing azeotropes in multicomponent mixtures." Computers & Chemical Engineering 17, no. 12 (December 1993): 1141–55. http://dx.doi.org/10.1016/0098-1354(93)80095-5.

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21

Okasinski, Matthew J., and Michael F. Doherty. "Thermodynamic behavior of reactive azeotropes." AIChE Journal 43, no. 9 (September 1997): 2227–38. http://dx.doi.org/10.1002/aic.690430909.

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22

Maier, Robert W., Joan F. Brennecke, and Mark A. Stadtherr. "Reliable computation of homogeneous azeotropes." AIChE Journal 44, no. 8 (August 1998): 1745–55. http://dx.doi.org/10.1002/aic.690440806.

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23

Zemmouri, Fayza, Hakim Madanı, Imad Anoune, and Abdelkrim Merzouguı. "Calculation of Azeotropic Properties for Ternary Mixtures with the PC-SAFT Equation of State." International Journal of Thermodynamics 27, no. 2 (June 1, 2024): 43–58. http://dx.doi.org/10.5541/ijot.1368434.

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In this study, a novel approach employing the Perturbed-Chain Statistical Associating Fluid Theory (PC-SAFT) Equation of State was introduced to investigate azeotropic behavior in ternary mixtures and explore their liquid-vapor equilibria. The temperature range spans (243.15323.5) K, covering a broad spectrum of conditions relevant to industrial and chemical processes. Our analysis focuses on six different ternary mixtures: Difluoromethane (R32) + 1,1-difluoroethane (R152a) + 2,3,3,3-tetrafluoropro-1-ene (R1234yf); Isobutane (R600a) + 1,1-difluoroethane (R152a) + 1,1,2,2-tetrafluoroethane (R134); 1,1,1,2-tetrafluoroethane (R134a) + 2,3,3,3-tetrafluoropro-1-ene (R1234yf) + isobutane (R600a); 1,1,1,2-tetrafluoroethane (R134a) + 2,3,3,3-tetrafluoropro-1-ene (R1234yf) + dimethyl ether (DME); isobutene (R600a) + 1,3,3,3-tetrafluoropropene (R12345ze(E)) + trifluoroiodomethane (R13I1); and difluoromethane (R32) + fluoroethane (R161) + 1,3,3,3-tetrafluoropropene (R1234ze(E)). Among these, only three mixtures exhibit azeotropic behavior. The PC-SAFT equation of state, incorporating an expansion form tailored for Vapor-Liquid Equilibrium (VLE) calculations within ternary mixtures, determined azeotropic composition and pressure based on the Gibbs-Konovalov theorem, which characterizes azeotropic behavior under constant temperature. Our estimations of the VLE and azeotropic composition and pressure closely align with experimental data. The maximum relative error in pressure does not exceed 4.2% for the R600a + R152a + R134 mixture and remains less than 6.56% for the liquid composition of R1234ze(E) within the (R600a + R1234ze(E) + R13I1) ternary mixture. These results underscore the reliability and accuracy of the PC-SAFT equation of state in modeling azeotropes within ternary mixtures.

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24

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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25

Faramarzi, Zohreh, Fatemeh Abbasitabar, Jalali Jahromi, and Maziar Noei. "New structure-based models for the prediction of normal boiling point temperature of ternary azeotropes." Journal of the Serbian Chemical Society 86, no. 7-8 (2021): 685–98. http://dx.doi.org/10.2298/jsc210218035f.

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Recently, development of the QSPR models for mixtures has received much attention. The QSPR modelling of mixtures requires the use of the appropriate mixture descriptors. In this study, 12 mathematical equations were considered to compute mixture descriptors from the individual components for the prediction of normal boiling points of 78 ternary azeotropic mixtures. Multiple linear regression (MLR) was employed to build all QSPR models. Memorized_ ACO algorithm was employed for subset variable selection. An ensemble model was also constructed using averaging strategy to improve the predictability of the final QSAR model. The models have been validated by a test set comprised of 24 ternary azeotropes and by different statistical tests. The resulted ensemble QSPR model had R2 training, R2 test and q2 of 0.97, 0.95, and 0.96, respectively. The mean absolute error (MAE), as a good indicator of model performance, were found to be 3.06 and 3.52 for training and testing sets, respectively.

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26

BARDUHN, ALLEN J. "THE EFFECT OF PRESSURE ON AZEOTROPES." Chemical Engineering Communications 38, no. 1-2 (October 1985): 9–16. http://dx.doi.org/10.1080/00986448508911292.

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27

Eckert, E., and M. Kubíček. "Computing heterogeneous azeotropes in multicomponent mixtures." Computers & Chemical Engineering 21, no. 3 (November 1997): 347–50. http://dx.doi.org/10.1016/s0098-1354(96)00001-4.

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28

Qi and Kai Sundmacher. "Geometrically Locating Azeotropes in Ternary Systems." Industrial & Engineering Chemistry Research 44, no. 10 (May 2005): 3709–19. http://dx.doi.org/10.1021/ie049031j.

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29

Jalilian, M. R. "Spectra and structure of binary azeotropes." Spectrochimica Acta Part A: Molecular and Biomolecular Spectroscopy 66, no. 1 (January 2007): 91–93. http://dx.doi.org/10.1016/j.saa.2006.02.028.

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30

Jalilian, M. R. "Spectra and structure of binary azeotropes." Spectrochimica Acta Part A: Molecular and Biomolecular Spectroscopy 66, no. 4-5 (April 2007): 976–78. http://dx.doi.org/10.1016/j.saa.2006.05.009.

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31

Jalilian, M. R. "Spectra and structure of binary azeotropes." Spectrochimica Acta Part A: Molecular and Biomolecular Spectroscopy 69, no. 3 (March 2008): 812–15. http://dx.doi.org/10.1016/j.saa.2007.05.032.

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32

Jalilian, M. R., and L. Alibabaei. "Spectra and structure of binary azeotropes." Spectrochimica Acta Part A: Molecular and Biomolecular Spectroscopy 62, no. 1-3 (November 2005): 322–25. http://dx.doi.org/10.1016/j.saa.2004.12.046.

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33

Maier, R. W., J. F. Brennecke, and M. A. Stadtherr. "Computing Homogeneous Azeotropes Using Interval Analysis." Chemical Engineering & Technology 22, no. 12 (December 1999): 1063–67. http://dx.doi.org/10.1002/(sici)1521-4125(199912)22:12<1063::aid-ceat1063>3.0.co;2-z.

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34

Liu, Gui Lian, Li Jun Wang, and Hao Li. "Study on the Volatility Order of Systems with Two Minimum Azeotropes." Advanced Materials Research 396-398 (November 2011): 261–66. http://dx.doi.org/10.4028/www.scientific.net/amr.396-398.261.

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In systems with two minimum binary azeotropes, there are two isovolatility lines. Different volatility order can be obtained according to different isovolatility lines. The volatility orders of components are identified according to the isovolatility lines and are compared with that identified based on the rigorous simulation using Aspen Plus. The results show that, in the system with two minimum binary azeotropes and two isovolatility lines, the volatility order of components is determined by the isovolatility line passing through the unstable node. Based on this, the rule for identifying the volatility order is proposed. The case studies show that this rule is simple and feasible.This template explains and demonstrates how to prepare your camera-ready paper for Trans Tech Publications. The best is to read these instructions and follow the outline of this text.

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35

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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36

Kim, M. S., W. J. Mulroy, and D. A. Didion. "Performance Evaluation of Two Azeotropic Refrigerant Mixtures of HFC-134a With R-290 (Propane) and R-600a (Isobutane)." Journal of Energy Resources Technology 116, no. 2 (June 1, 1994): 148–54. http://dx.doi.org/10.1115/1.2906020.

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The reduction in chlorofluorocarbon (CFC) and hydrochlorofluorocarbon (HCFC) production and the scheduled phase-out of these ozone-depleting refrigerants require the development and determination of environmentally safe refrigerants for use in heat pumps, water chillers, air conditioners, and refrigerators. This paper presents a performance evaluation of a generic heat pump with two azeotropic refrigerant mixtures of HFC-134a (1,1,1,2-tetrafluoroethane) with R-290 (propane) and R-600a (isobutane); R-290/134a (45/55 by mass percentage) and R-134a/600a (80/20 by mass percentage). The performance characteristics of the azeotropes were compared with pure CFC-12, HFC-134a, HCFC-22, and R-290 at the high temperature cooling and heating conditions including those using liquid-line/suction-line heat exchange. The coefficient of performance of R-290/134a is lower than that of HCFC-22 and R-290, and R-134a/600a shows higher coefficient of performance than CFC-12 and HFC-134a. The capacity for R-290/134a is higher than that for HCFC-22 and R-290, and R-134a/600a exhibits higher system capacity than CFC-12 and HFC-134a. Experimental results show that the discharge temperatures of the studied azeotropic mixtures are lower than those of the pure refrigerants, CFC-12 and HCFC-22.

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37

Wyczesany, Andrzej. "Simulation of N-Propanol Dehydration Process Via Heterogeneous Azeotropic Distillation Using the NRTL Equation." Chemical and Process Engineering 38, no. 1 (March 1, 2017): 163–75. http://dx.doi.org/10.1515/cpe-2017-0013.

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Abstract Numerical values of the NRTL equation parameters for calculation of the vapour - liquid - liquid equilibria (VLLE) at atmospheric pressures have been presented for 5 ternary mixtures. These values were fitted to the experimental VLLE and vapour - liquid equilibrium (VLE) data to describe simultaneously, as accurately as possible, the VLE and the liquid - liquid equilibria (LLE). The coefficients of this model called further NRTL-VLL were used for simulations of n-propanol dehydration via heterogeneous azeotropic distillation. The calculations performed by a ChemCAD simulator were done for 4 mixtures using hydrocarbons, ether and ester as an entrainer. In majority simulations the top streams of the azeotropic column had composition and temperature similar to the corresponding experimental values of ternary azeotropes. The agreement between the concentrations of both liquid phases formed in a decanter and the experimental values of the LLE was good for all four simulations. The energy requirements were the most advantageous for the simulation with di-npropyl ether (DNPE) and isooctane. Simulations were performed also for one mixture using the NRTL equation coefficients taken from the ChemCAD database. In that case the compositions of the liquid organic phases leaving the decanter differed significantly from the experimental LLE data.

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38

Sheybani, Shima, and Behrooz Mahmoodzadeh Vaziri. "Three-Phase Distillation of Ethyl Acetate/Water/Ethanol: Separation Feasibility and Conceptual Design." Chemistry & Chemical Technology 16, no. 2 (June 15, 2022): 237–54. http://dx.doi.org/10.23939/chcht16.02.237.

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Continuous production of ethyl acetate involves various separation challenges due to multiple azeotropes. In this study, three-phase advanced distillation method is applied through diverse purification scenarios for ternary separation of ethyl acetate system (ethyl acetate/water/ethanol). This highly non-ideal mixture contains four azeotropes and three distillation regions. To select the best distillation region, the separation feasibility and conceptual design of ethyl acetate three-phase distillation unit are comprehensively investigated by the extended boundary value method for various feed locations and numerous product recoveries. It was found that the region in which ethanol is a stable component was the most suitable region for the distillation process. Further, the conceptual design of the three-phase column is optimized by variation of reflux ratio and operating pressure. Ultimately, based on the conceptual design results, rigorous simulation of the process is accomplished and ethanol is separated with 99.25 mol % purity.

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39

Frey, Th, and J. Stichlmair. "Reactive Azeotropes in Kinetically Controlled Reactive Distillation." Chemical Engineering Research and Design 77, no. 7 (October 1999): 613–18. http://dx.doi.org/10.1205/026387699526656.

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40

Harding, S. T., C. D. Maranas, C. M. McDonald, and C. A. Floudas. "Locating All Homogeneous Azeotropes in Multicomponent Mixtures." Industrial & Engineering Chemistry Research 36, no. 1 (January 1997): 160–78. http://dx.doi.org/10.1021/ie960305f.

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Thakore, Jashwantsinh L., and Gerald D. Holder. "Solid vapor azeotropes in hydrate-forming systems." Industrial & Engineering Chemistry Research 26, no. 3 (March 1987): 462–69. http://dx.doi.org/10.1021/ie00063a011.

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42

Lynn, Scott, and Donald N. Hanson. "Multieffect extractive distillation for separating aqueous azeotropes." Industrial & Engineering Chemistry Process Design and Development 25, no. 4 (October 1986): 936–41. http://dx.doi.org/10.1021/i200035a017.

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43

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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44

Okasinski, M. J., and M. F. Doherty. "Prediction of heterogeneous reactive azeotropes in esterification systems." Chemical Engineering Science 55, no. 22 (November 2000): 5263–71. http://dx.doi.org/10.1016/s0009-2509(00)00153-6.

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Chen, Geng-Hua, Qi Wang, Lian-Zhong Zhang, Jian-Bin Bao, and Shi-Jun Han. "Study and applications of binary and ternary azeotropes." Thermochimica Acta 253 (April 1995): 295–305. http://dx.doi.org/10.1016/0040-6031(94)02078-3.

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46

Ma, Yixin, Kang Ma, Huixin Wang, Xueli Geng, Jun Gao, Zhaoyou Zhu, and Yinglong Wang. "QSPR modeling of azeotropic temperatures and compositions for binary azeotropes containing lower alcohols using a genetic function approximation." Chinese Journal of Chemical Engineering 27, no. 4 (April 2019): 835–44. http://dx.doi.org/10.1016/j.cjche.2018.06.031.

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47

Kruber, Kai Fabian, and Mirko Skiborowski. "Topology-Based Initialization for the Optimization-Based Design of Heteroazeotropic Distillation Processes." Processes 10, no. 8 (July 28, 2022): 1482. http://dx.doi.org/10.3390/pr10081482.

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Distillation-based separation processes, such as extractive or heteroazeotropic distillation, present important processes for separating azeotropic mixtures in the chemical and biochemical industry. However, heteroazeotropic distillation has received much less attention than extractive distillation, which can be attributed to multiple reasons. The phase equilibrium calculations require a correct evaluation of phase stability, while the topology of the heterogeneous mixtures is generally more complex, comprising multiple azeotropes and distillation regions, resulting in an increased modeling complexity. Due to the integration of distillation columns and a decanter, even the simulation of these processes is considered more challenging, while an optimal process design should include the selection of a suitable solvent, considering the performance of the integrated hybrid process. Yet, the intricate mixture topologies largely impede the use of simplified criteria for solvent selection. To overcome these limitations and allow for a process-based screening of potential solvents, the current work presents a topology-based initialization and optimization approach for designing heteroazeotropic distillation processes. The systematic initialization enables an efficient evaluation of different solvents with different mixture topologies, which is further exploited for optimization-based sensitivity analysis and multi-objective optimization. Three case studies are analyzed with about 170 individually optimized process designs, including stage numbers, feed locations, phase ratios, and heat duties.

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Reis, M. H. M., L. F. S. Mascolo, and M. R. Wolf-Maciel. "Development of a robust algorithm to compute reactive azeotropes." Brazilian Journal of Chemical Engineering 23, no. 3 (September 2006): 395–403. http://dx.doi.org/10.1590/s0104-66322006000300013.

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Palaniappan, L., and S. Nithiyanantham. "Acoustical and physico-chemical study of binary azeotropes (aniline)." Journal of Molecular Liquids 312 (August 2020): 113423. http://dx.doi.org/10.1016/j.molliq.2020.113423.

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50

Wasylkiewicz, Stanislaw K., Michael F. Doherty, and Michael F. Malone. "Computing All Homogeneous and Heterogeneous Azeotropes in Multicomponent Mixtures." Industrial & Engineering Chemistry Research 38, no. 12 (December 1999): 4901–12. http://dx.doi.org/10.1021/ie990214t.

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