Relevant bibliographies by topics / Azeotropic point

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Academic literature on the topic 'Azeotropic point'

Author: Grafiati
Published: 4 June 2021
Last updated: 11 February 2022

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Journal articles on the topic "Azeotropic point"

1

Wang, Xuehui, Tiannian Zhou, Qinpei Chen, Junjiang He, Zheng Zhang, and Jian Wang. "Experimental study on combustion characteristics of blended fuel pool fires." Journal of Fire Sciences 37, no. 3 (May 2019): 236–56. http://dx.doi.org/10.1177/0734904119839917.

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Liquid–vapor phase equilibrium theories are used to analyze boiling processes of blended fuel pool fires, and the results show that there are two boiling mechanisms (azeotropism and non-azeotropism) for blended fuels compared with single-component fuels. A series of pool fire experiments were conducted to investigate the combustion characteristics of blended fuel pool fires. The experimental results showed that the two boiling mechanisms have different effects on the burning process of the fuel blends. The boiling temperature and composition varied for the non-azeotropic blends during the burning process and remained steady for azeotropic blends. Furthermore, the boiling temperature of azeotropic blends is lower than that of its components and ranges from a specific temperature to the boiling point of the less volatile component. The flame radiant fraction of the azeotropic blend was also relatively constant during the burning process, whereas that of the non-azeotropic blend varied in different stages of the burning process. Heskestad’s flame height model and flame axial temperature distribution model are applicable for pool fires of azeotropic and non-azeotropic blends.
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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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3

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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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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Yanyu, Liang. "Sufficient Conditions for Existence of the Azeotropic Point." University Chemistry 30, no. 1 (2015): 82–88. http://dx.doi.org/10.3866/pku.dxhx20150117.

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6

Moad, G., DH Solomon, TH Spurling, and DJ Vearing. "Critical-Points (Azeotropic Compositions) in Multicomponent Copolymerization." Australian Journal of Chemistry 39, no. 11 (1986): 1877. http://dx.doi.org/10.1071/ch9861877.

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The necessary and sufficient conditions for the existence of critical points ( azeotropic compositions) in multicomponent copolymerization are defined, and the preferred method for calculating critical points for a given set of reactivity ratios is provided. This method offers considerable advantages in both simplicity and computation speed over methods already in the literature. A computer program for performing the calculation on systems with up to 10 components is briefly described. Approximate probabilities for the existence of critical points in ternary and quaternary systems have been evaluated as a function of whether binary critical points exist for pairs of the monomers involved. These data show that, contrary to the widely held view, in systems of three or more components all rij > 1 or all rij < 1is neither a necessary nor a sufficient condition for the existence of a critical point. Those systems which always and those systems which never give rise to critical points are indicated.
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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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Hartanto, Dhoni, Prima Astuti Handayani, Akhmad Sutrisno, Viona Widya Anugrahani, Asalil Mustain, and Ianatul Khoiroh. "Isopropyl Alcohol Purification through Extractive Distillation using Glycerol as an Entrainer: Technical Performances Simulation and Design." Jurnal Bahan Alam Terbarukan 8, no. 2 (December 31, 2019): 133–43. http://dx.doi.org/10.15294/jbat.v8i2.23477.

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Isopropyl alcohol is widely used as industrial chemical intermediates and common solvents in households, pharmaceuticals, food, cosmetics, and medical purposes. The high purity of isopropyl alcohol requires special separation from its impurity i.e. water due to isopropyl alcohol and water form an azeotropic point, which is difficult to separate using a conventional distillation method. The azeotropic point of this mixture is at isopropyl alcohol mole fraction of 0.68 and temperature of 353.4 K. One of the optimum methods to separate an azeotrope point is through the extractive distillation which use a third component as a solvent. Glycerol is one of the solvents which can be used as a potential entrainer in the extractive distillation. Glycerol is produced in the biodiesel production as a by-product. Moreover, glycerol is an eco-friendly chemical. In this work, the simulation of the extractive distillation of isopropyl alcohol/water system with glycerol as an entrainer was simulated using Aspen Plus. The Non-Random Two-Liquid (NRTL) model was used as thermodynamic model in the simulation. The effect of stage number, binary feed stage, entrainer feed stage, and reflux ratio to the purity of isopropyl alcohol, and reboiler-condenser duties were examined to achieve the optimum design for the extractive distillation column with less energy requirements. The simulation results showed that the optimum configurations in the extractive distillation column design are at 25 theoretical stages, binary feed stage (BFS) of 20, entrainer feed stage (EFS) of 2, and reflux ratio (RR) of 0.5 to produce isopropyl alcohol with the purity of 99.27%. The design and sizing of the extractive distillation column were also proposed in this work.
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Moad, G., DH Soloman, TH Spurling, and DJ Vearing. "Critical Points in Binary Copolymerization and the Penultimate Group Effect." Australian Journal of Chemistry 38, no. 9 (1985): 1287. http://dx.doi.org/10.1071/ch9851287.

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In order to examine the influence that a penultimate group effect can have on the number and magnitude of critical points ( azeotropic compositions) in binary copolymerization an expression for the critical point(s) has been derived. Analysis of this relationship shows that in a situation where one critical point would have been expected on the basis of terminal-model kinetics (no penultimate group effect) a modest penultimate group effect can mean that zero, one or three critical points may exist, or, in systems where no critical points would have been predicted, two critical points may exist.
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10

Hiaki, Toshihiko, Katsumi Tochigi, and Kazuo Kojima. "Measurement of vapor-liquid equilibria and determination of azeotropic point." Fluid Phase Equilibria 26, no. 1 (January 1986): 83–102. http://dx.doi.org/10.1016/0378-3812(86)85006-3.

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Dissertations / Theses on the topic "Azeotropic point"

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Zhou, Xiaoqin. "Evaluation of instantaneous and cumulative models for reactivity ratio estimation with multiresponse scenarios." Thesis, Waterloo, Ont. : University of Waterloo, 2004. http://etd.uwaterloo.ca/etd/x5zhou2004.pdf.

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Thesis (M.A.Sc.)--University of Waterloo, 2004.
"A thesis presented to the University of Waterloo in fulfillment of the thesis requirement for the degree of Master of Applied Science in Chemical Engineering". Includes bibliographical references. Issued also in PDF fomat and available via the World Wide Web. Requires internet connectivity, World Wide Web browser, and Adobe Acrobat Reader to view and print files.
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Modise, Tshepo Sehole David. "Experimental simulation of distillation column profile maps." Thesis, 2008. http://hdl.handle.net/10539/4713.

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ABSTRACT One of the most important tasks in the chemical industry is the separation of multicomponent liquid mixtures into one or more high-purity products. Several technologies are feasible for this task, either alone or in combination, such as distillation, extraction, crystallization, ect. Among these, distillation is by far the most widely spread and has a long history in chemical technology. However, until recently, there has been no systematic approach for understanding the separation of complex mixtures where azeotropes and multiple liquid phases may occur. There has been a growing interest in the use of residue curve and column profiles for the preliminary design of distillation columns. Residue curves and column profile are not only used to predict the composition changes in the distillation column but also to determine the feasibility of the proposed separation. Recently, theory underlying column profile maps has been developed by Tapp, Holland and co-workers. However there has been no direct experimental validation of the predictions of the column profile map theory. The main aim of this thesis is to experimentally verify some of the predictions of column profile map theory. A simple experimental batch apparatus has been developed to measure residue curve maps (RCMs) by Tapp and co-workers, the apparatus was modified so that it could be used to measure column profile maps (CPMs) in this thesis. CPM theory has shown that CPMs are linear transforms of the residues curve maps (RCMs). A stable node which was the apex of a mass balance triangle (MBT) was introduced inside the MBT, this was done by transforming the RCMs to CPMs using the appropriate distillate composition xd and reflux ratio R. It was also shown that the saddle point which was on the boundary of the triangle of the RCM can be shifted inside the MBT by transforming the RCM to CPM. This is again in accordance with theoretical predictions of CPM theory. iv Residue curves (RCs) and pinch point curves (PPCs) are used to determine the operation leaves and hence the feasible region for distillation columns operating at a specific distillate and bottoms composition for all fixed reflux ratio. The operating leaves were expanded beyond the pinch point curve by varying the reflux ratio from a higher reflux to a lower reflux ratio. This showed that one can effectively cross the pinch point curve hence expanding the operating leave. Finally the importance of experimentally measuring CPMs is demonstrated. Two thermodynamic models were used to predict the profiles of a complex system. The binary vapor-liquid equilibrium (VLE) diagrams and the residue curves produced from using these two thermodynamic models did not predict the same topology. The composition of the profiles were not the same because there were multiple liquid phases involved in this system, which made it difficult for the researchers to measure the correct profiles. Column profile maps were simulated using the different thermodynamic models, they also showed that there is some discrepancy between the predictions of the two models.
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Conference papers on the topic "Azeotropic point"

1

Smit, F. J., and Josua P. Meyer. "An Analytical Comparison Between the Performance of a Hot Water Heat Pump With a Non-Azeotropic Refrigerant Mixture and a Pure Refrigerant." In ASME 1997 Turbo Asia Conference. American Society of Mechanical Engineers, 1997. http://dx.doi.org/10.1115/97-aa-042.

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The applications of hot water in the industrial, domestic and mining applications are numerous, and these are only a few of the core areas of use. In these applications fossil fuels and electrical resistance systems are usually used to heat water to temperatures near boiling point. The refrigerant R22, that is currently being used in hot water heat pumps, delivers hot water temperatures from 60 °C to 65 °C. This limits the applications of hot water heat pumps. This analytical study uses three comparison methods to investigate and compare the potential of a non-azeotropic refrigerant mixture consisting of R22 and R142b. From the results different advantages of non-azeotropic refrigerant mixtures are evident. Depending on the application, if the results of a non-azeotropic refrigerant mixture are compared with a pure R22 heat pump, an increase in hot water temperatures to above boiling point, an increase in coefficient of performance, an increase in capacity and a decrease in compressor pressure ratio are possible. Unfortunately, not all these advantages are valid for each application. For instance, extremely high hot water temperatures are obtained, whilst the heating capacity is excessively low.
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Lupo, Giandomenico, and Christophe Duwig. "A Numerical Study of Ethanol-Water Droplet Evaporation." In ASME Turbo Expo 2017: Turbomachinery Technical Conference and Exposition. American Society of Mechanical Engineers, 2017. http://dx.doi.org/10.1115/gt2017-64420.

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The present effort focuses on detailed numerical modelling of the evaporation of an ethanol-water droplet. The model intends to capture all relevant details of the process: it includes species and heat transport in the liquid and gas phases, and detailed thermo-physical and transport properties, varying with both temperature and composition. Special attention is reserved to the composition range near and below the ethanol/water azeotrope point at ambient pressure. For this case, a significant fraction of the droplet lifetime exhibits evaporation dynamics similar to those of a pure droplet. The results are analysed and model simplifications are examined. In particular, the assumptions of constant liquid properties, homogeneous liquid phase composition and no differential volatility may not be valid depending on the initial droplet temperature.
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Kale, Kaustubh S., and Sunil S. Mehendale. "Novel Application-Specific Methodology for the Assessment of Microfin Tube Condensation Heat Transfer Correlations." In ASME 2015 International Mechanical Engineering Congress and Exposition. American Society of Mechanical Engineers, 2015. http://dx.doi.org/10.1115/imece2015-51908.

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Extensive critical study of five popular microfin tube correlations for condensation heat transfer coefficients (HTCs) was carried out. The principal aim of this investigation was to develop an application-specific quantitative tool to assess the predictive accuracy and applicability of these correlations for halogenated refrigerants as well as CO2. This novel methodology was developed and validated against a dataset of 1163 experimental data points for CO2, R22, R134a, R410A, R407C, R125 and other halogenated refrigerants obtained from a large number of published works which included diverse microfin tube geometries and condensing conditions. The tool will enable the engineer or experimentalist to select the best (i.e., most accurate) condensation HTC correlation for a given microfin tube application, thereby significantly reducing tube testing costs, leading to lower turn-around times and more efficient designs. Based on the analysis carried out using the new methodology, it was found that overall, Cavallini et al. (2009) was the most widely applicable and accurate flow condensation correlation. Yu and Koyama (1998) was found to perform well for CO2, 7 mm and smaller tubes and low helix angles (5° to 10°). Interestingly, Cavallini et al. (2009), Yu and Koyama (1998) and Chamra et al. (2005) were found to predict the HTC satisfactorily for zeotropic refrigerants such as R407C, although their development was based on pure and near-azeotropic refrigerants only. The Han and Lee (2005) correlation was found to be inaccurate over most of the data set and therefore has a very low probability of being recommended for any application.
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Rossetti, Ilenia, Cesare Biffi, Lucio Forni, Gian Franco Tantardini, Giuseppe Faita, Mario Raimondi, Edoardo Vitto, and Davide Alberti. "Integrated 5 kWe + 5 kWt PEM-FC Generator From Bioethanol: A Demonstrative Project." In ASME 2010 8th International Conference on Fuel Cell Science, Engineering and Technology. ASMEDC, 2010. http://dx.doi.org/10.1115/fuelcell2010-33049.

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A power unit constituted by a reformer, a H2 purification section and a fuel cell is being installed c/o the Dept. of Physical Chemistry and Electrochemistry of Universita` degli Studi di Milano, on the basis of a collaboration with Helbio S.A. (Hydrogen and Energy Production Systems, supplier) and the support of some sponsors (Linea Energia S.p.A., Parco Tecnologico Padano and Provincia di Lodi). The system is suitable to obtain 5 kWelectric (a.c.) + 5 kWthermal (hot water at 70°C) as peak output. H2 is produced by steam reforming (SR) of second generation bioethanol, obtainable by different non-food competitive biomass. The assessment of the effect of biomass nature and of the consequent different impurities left in the produced bioethanol is part of the experimentation, together with the evaluation of the impact of bioethanol production cost on the final energy cost. Furthermore, the effect of different ethanol/steam ratios will be taken into account to lighten as much as possible the energy demanding ethanol dehydration process. The former point focuses on catalyst life, imposing careful ethanol characterisation and proper catalyst formulation, whereas the latter is connected with the overall energetic efficiency and economic sustainability. Indeed, the reforming process requires co-feeding of water, opening the way to the research of different, cheaper, ethanol purification strategies, leading to lower ethanol concentration with respect to the azeotrope. The reformate is purified from CO down to a concentration below 20 ppm, suitable to feed the proton exchange membrane fuel cells (PEMFC) stack integrated in the fuel processor. This result is achieved by feeding it to two water gas shift reactors, connected in series and operating at high and low temperature, respectively. The expected CO concentration in the outcoming gas is ca. 1 vol% and the final CO removal to meet the specifications is accomplished by selective methanation. The purified H2 is fed to a 5 kWe PEMFC stack, which should have an expected overall efficiency around 80% (including thermal output). The main goal of the present project is to check system performance under widely different operating conditions and load, to verify the effectiveness of the proposed technology and to suggest adequate improvements. Different operating conditions are under evaluation as for ethanol origin, purity, concentration, temperature and space velocity of every reaction step, so to obtain the best compromise between H2 yield, power output and operating costs.
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