Phase equilibria properties of binary and ternary systems containing isopropyl ether + isobutanol + benzene at K.
|
|
- Franklin Newton
- 5 years ago
- Views:
Transcription
1 Phase equilibria properties of binary and ternary systems containing isopropyl ether + isobutanol + benzene at K. R.M. Villamañán 1, M.C. Martín 2, C.R. Chamorro 2, M.A. Villamañán 2, J.J. Segovia 2 1 Dpto. de Didáctica de las Ciencias Sociales y Eperimentales, Escuela Universitaria de Educación, Campus Universitario de Palencia. E Palencia, Spain. 2 Laboratorio de Termodinámica y Calibración TERMOCAL, E.T.S. de Ingenieros Industriales Universidad de Valladolid, E Valladolid, Spain, osseg@eis.uva.es. Abstract Isothermal vapour-liquid equilibrium data have been measured for the ternary system (isopropyl ether + isobutanol + benzene) and two of the binary systems involved (isopropyl ether + isobutanol) and (isobutanol + benzene) at K. A static technique consisting of an isothermal total pressure cell was used for the measurements. Data reduction by Barker's method provides correlations for G E using the Margules equation for the binary systems and the Wohl epansion for the ternary system. Wilson, NRTL and UNIQUAC models have been applied successfully to both the binary and the ternary systems. Keywords:VLE data, ternary mitures, isopropyl ether (DIPE), isobutanol, benzene 1. Introduction. Ethers and alcohols have been traditionally used as blending agents in the formulation of new gasolines for enhancing the octane number. To better understand and model these unleaded gasolines we started many years ago a research program on the thermodynamic characterization of ternary mitures, as the simplest multicomponent system, containing oygenated additives (ethers and alcohols) and different type of hydrocarbons (paraffins, cycloparaffins, aromatics, oleffins). Methyl tert-butyl ether (MTBE), tert-amylmethyl ether (TAME) and isopropyl ether (DIPE) were chosen as representative ethers; methanol, isopropanol, 1-propanol, and tert-amyl alcohol as alcohol additives. Now, we continued studying ternary mitures containing DIPE, benzene and different butanol isomers. Here, we report vapour-liquid equilibrium data concerning the ternary miture DIPE + isobutanol + benzene at K. The eperimental technique used is a static type of high accuracy. These highest quality of vapour-liquid equilibrium data are required to improve the interaction parameters of the predictive models which are used in process simulation packages. The accuracy of a process simulation depends strongly on the thermodynamic models used to describe the physical behaviour of the involved components. Both purposes are carried out with these measurements. 2. Eperimental. All the chemicals used were purchased from Fluka Chemie AG and were of the highest purity available, chromatography quality reagents (of the series puriss. p.a.) with a purity >99.5 (G.C.). All liquids degassed prior to measurements using a modified distillation method based on the technique of Van Ness and Abbott [1], under vacuum. The purities of the chemicals were checked by gas chromatography and were found to be >99.5 for all the
2 compounds. In Table 1, the vapour pressures of the pure constituents measured in this work are compared with those reported in the literature as a check for complete degassing. Table 1 Average values of eperimental vapor pressures (P s i ) for the pure compounds measured in this work, and literature values (P s i ) (lit.) at T = K. DIPE (i=1) Iso-butanol (i=2) Benzene (i=3) s p i /(kpa) p s i (lit.) /(kpa) a c a,e b d f a Reported by Chamorro et al. [4] b Reported by Ambrose et al. [11] c Reported by Ambrose et al. [12] d Reported by Garriga et al. [13] e Reported by Garriga et al. [14] f Reported by Oracz [15] An isothermal total pressure cell has been employed for measuring the vapour-liquid equilibrium of binary and ternary mitures. The apparatus and static measuring technique are based on that by Van Ness and has been described in detail in the literature [2,3]. The equilibrium properties measured directly and their uncertainties are: inected volume ±0.03 ml, temperature ±10 mk and total pressure ±5 Pa. Eperimental values of total vapour pressure for the binary mitures are obtained in two overlapping runs starting from opposite ends of the composition range; for the ternary miture they are obtained by adding a third component up to a mole fraction of = 0.5, to a binary miture with a mole fraction of one component close to = (0.3, or 0.7), si dilution lines were carried out. 3. Results and discussion. In this work, they are reported eperimental isothermal P--y data for the ternary system di-isopropyl ether (DIPE) + isobutanol + benzene and two of the binary systems involved DIPE +isobutanol and benzene + isobutanol at K. The other binary system has been measured and published before.[4] Data reduction for the binary and ternary mitures was done by Barker s method according to well established procedures [5,6]. The non-ideality of the vapour phase was taken into account with the virial equation of state, truncated after the second term. Data for the ternary system is adequately correlated by the three-parameter Wohl equation [7]: E Gm g = = g + g + g + ( C + C + C (1) ) RT which also includes the parameters of the corresponding binaries g i, according to equation (2). The adustable parameters C 0, C 1 and C 2 are found by regression of the ternary data. Correlations for g i are given by a five-parameter Margules equation of the following form: g i = RT G E m 2 2 = { Ai i Ai ( λ i i + λi ) i + η i } i (2) The binary and ternary systems have also been correlated using Wilson [8], NRTL [9] and UNIQUAC [10] models. The data correlation results for the binary systems reported here are
3 summarized in table 2, including, for convenience, those of (DIPE + Benzene), which have been reported previously [4]. Table 2 Determined parameters of the models used for the binary subsystems of ternary system Di-isopropyl ether (1) + isobutanol (2) + benzene(3) at T= K, together with the root mean square deviation of pressure ( r.m.s.d. p) and the maimum value of the deviation (ma p ). The p term is defined as the difference between the eperimental and calculated pressure. Margules Wilson NRTL UNIQUAC Di-isopropyl ether (1) + iso-butanol (2) A A λ λ η α r.m.s.d. p/kpa ma p /kpa Benzene (1) + iso-butanol (2) A A λ λ η α r.m.s.d. p/kpa ma p /kpa Di-isopropyl ether (1) + Benzene (2) a A A λ 12 =λ α r.m.s.d. p/kpa ma p /kpa a Data published in ref.[4] All the models fit quite good both binary systems however slight better results are obtained for the five-parameter Margules equation. The root mean square deviation between eperimental and calculated pressure is 9 Pa with a maimum deviation of 16 Pa for (DIPE + isobutanol) and they are 12 Pa and 18 Pa, respectively, for (benzene + isobutanol). Both binary systems present a large positive deviation from the ideality with a maimum value of the ecess molar Gibbs energy of 950 Jmol -1 for (benzene + isobutanol) and 585 Jmol -1 for (DIPE + isobutanol), which are located near isobutanol liquid mole fraction of Eperimental P- data for the binary systems are shown on figure 1 (a), the vapour compositions have been calculated by Margules equation. As an eample of the fits of models to the data, figure 1 (b), shows a plot of the pressure residuals versus liquid composition for both binary systems using five-parameters Margules equation. It shows how the model fits the data and also, the good agreement of eperimental pressure measured twice for compositions
4 P/kPa (Pcalc-Pep)/kPa , y1 (a) (b) Figure 1: (a) Total vapour pressure for binary systems as a function of the liquid, 1, and vapour compositions, y 1 : ( ) di-isopropyl ether (1) + isobutanol (2); ( ) benzene (1) + isobutanol (2); and ( ) di-isopropyl ether (1) + benzene (2). (b) Pressure residuals as a function of the liquid composition, 1 : ( ) di-isopropyl ether (1) + isobutanol (2); ( ) benzene (1) + isobutanol (2). For the ternary system correlation results are summarized in table 3 which contains the correlations parameters, the root mean square pressure deviation and the maimum value of this deviation. The good results of the fits from all the models are shown in the table, the root mean square pressure deviation varies between 23 Pa for Wohl epansion to 51 Pa for Wilson equation and the maimum value of the deviation is 174 Pa for Wilson equation. Table 3 Summary of the data reduction results obtained for the ternary system (DIPE (1) + isobutanol (2) + Benzene (3)) at K. Wilson NRTL UNIQUAC Wohl A C 0 = A C 1 = A C 2 = A A A α α α r.m.s.d. p/kpa ma p /kpa Results for the ternary system are also shown graphically in figure 2. They are plotted lines of constant total pressure and lines of constant ecess molar Gibbs energy for the ternary system calculated with Wohl epansion; eperimental data are also drawn in the figure. Total pressure of the ternary system varies from the lowest vapour pressure pure component (isobutanol) to the highest vapour pressure pure component (DIPE). On the other hand the maimum value of ecess molar Gibbs energy corresponds to the least ideal binary system.
5 (a) (b) Figure 3. Plots for the ternary system di-isopropyl ether (1) + isobutanol (2) + benzene (3) at K as a function of liquid composition, i,. (a) Isobar lines in kpa (b) Iso-G E lines in Jmol -1. List of symbols A i, A i adustable parameters of the correlation models C 0, C 1, C 2 parameters in Eq. (1) G E molar ecess Gibbs energy (Jmol -1 ) i, constituent identification: 1, 2 or 3 P total pressure (kpa) s P i vapour pressure of pure constituent i (kpa) rmsd root mean square pressure deviation mole fraction, liquid phase y mole fraction, vapour phase Greek letters α i λ i η signifies difference parameter for NRTL model parameter for Margules equation parameter for Margules equation Acknowledgements Support for this work came from the Spanish Ministry of Science and Technology, proect PPQ C References [1] H.C. Van Ness, M.M. Abbott, Ind. Eng. Chem. Fundam. 17 (1978) [2] L M Lozano, E A Montero, M C Martín, M A Villamañán, Fluid Phase Equilib. 110 (1995) [3] J J Segovia, M C Martín, C R Chamorro, M A Villamañán, Fluid Phase Equilib. 133 (1997) [4] C R Chamorro, J J Segovia, M C Martín, M A Villamañán, Entropie 224/225 (1999) [5] M.M. Abbott, H.C. Van Ness, AIChE Journal 21 (1975) [6] M.M. Abbott, J.K. Floess, G.E. Walsh Jr. and H.C. Van Ness, AIChE Journal 21 (1975), [7] K. Wohl, Chem. Eng. Prog. 49 (1953) 218. [8] G.M. Wilson, J. Amer. Chem. Soc. 86 (1964) [9] H. Renon, J.M. Prausnitz, AIChE Journal 14 (1968) [10] D.S. Abrams, J.M. Prausnitz, AIChE Journal 21 (1975)
6 [11] D. Ambrose, J.H. Ellender, C.H.S. Sprake, R. Townsend, J. Chem. Thermodyn. 8 (1976) [12] D. Ambrose, N. B. Ghiassee, J. Chem. Thermodyn. 19 (1987) [13] R. Garriga, S. Martínez, P. Pérez, M.Gracia, Fluid Phase Equilib. 181 (2001) [14] R. Garriga, P. Pérez, M.Gracia, Fluid Phase Equilib. 227 (2005) [15] P. Oracz, Int. Data Ser. Sel. Data Mitures 24 (1996) 280.
Vapor liquid equilibria for the binary system 2,2 dimethylbutane + 1,1 dimethylpropyl methyl ether (TAME) at , , and 338.
Fluid Phase Equilibria 221 (2004) 1 6 Vapor liquid equilibria for the binary system 2,2 dimethylbutane + 1,1 dimethylpropyl methyl ether (TAME) at 298.15, 318.15, and 338.15 K Armando del Río a, Baudilio
More informationFluid Phase Equilibria (2001)
Fluid Phase Equilibria 187 188 (2001) 299 310 Vapor liquid equilibria for the binary systems decane + 1,1-dimethylethyl methyl ether (MTBE) and decane + 1,1-dimethylpropyl methyl ether (TAME) at 308.15,
More informationAgung Ari Wibowo, S.T, M.Sc THERMODYNAMICS MODEL
Agung Ari Wibowo, S.T, M.Sc THERMODYNAMICS MODEL THERMODYNAMICS MODEL For the description of phase equilibria today modern thermodynamic models are available. For vapor-liquid equilibria it can bedistinguished
More informationIntroduction (1) where ij denotes the interaction energy due to attractive force between i and j molecules and given by; (2)
(7)7 Prediction of Vapor-Liquid Equilibria of Binary Systems Consisting of Homogeneous Components by Using Wilson Equation with Parameters Estimated from Pure-Component Properties Shigetoshi KOBUCHI, Kei
More informationFlash point of organic binary mixtures containing alcohols: experiment and prediction
Cent. Eur. J. Chem. 11(3) 2013 388-393 DOI: 10.2478/s11532-012-0171-6 Central European Journal of Chemistry Flash point of organic binary mixtures containing alcohols: experiment and prediction Research
More informationIsobaric Vapor Liquid Equilibria of Systems containing N-Alkanes and Alkoxyethanols
Isobaric Vapor Liquid Equilibria of Systems containing N-Alkanes and Alkoxyethanols Sunghyun Jang, Moon Sam Shin, Yongjin Lee, Hwayong Kim * School of Chemical Engineering & Institute of Chemical Processes,
More informationExtending the Van Laar Model to Multicomponent Systems
The Open Thermodynamics Journal, 010, 4, 19-140 19 Extending the Van Laar Model to Multicomponent Systems Open Access Ding-Yu Peng* Department of Chemical Engineering, University of Saskatchewan 57 Campus
More informationDETERMINATION AND PREDICTION OF THE ISOBARIC VAPOR- LIQUID-LIQUID EQUILIBRIUM DATA
DETERMINATION AND PREDICTION OF THE ISOBARIC VAPOR- LIQUID-LIQUID EQUILIBRIUM DATA Koichi Iwakabe and Hitoshi Kosuge Department of Chemical Engineering, Tokyo Institute of Technology 12-1, Ookayama-2,
More informationExtraction of Phenol from Industrial Water Using Different Solvents
Research Journal of Chemical Sciences ISSN 31-606X. Extraction of Phenol from Industrial Water Using Different Solvents Abstract Sally N. Jabrou Department of Radiology, Health and Medical Technical College
More informationStatus and results of group contribution methods
Pure & Appl. Cbem., Vol. 65, No. 5, pp. 919926, 1993. Printed in Great Britain. @ 1993 IUPAC Status and results of group contribution methods J. Gmehling, K. Fischer, J. Li, M. Schiller Universitat Oldenburg,
More informationMODELING OF PHASE EQUILIBRIA FOR BINARY AND TERNARY MIXTURES OF CARBON DIOXIDE, HYDROGEN AND METHANOL
MODELING OF PHASE EQUILIBRIA FOR BINARY AND TERNARY MIXTURES OF CARBON DIOXIDE, HYDROGEN AND METHANOL Neil R. Foster *, Keivan Bezanehtak, Fariba Dehghani School of Chemical Engineering and Industrial
More informationBoiling points for five binary systems of sulfolane with aromatic hydrocarbons at kpa
Fluid Phase Equilibria 190 (2001) 61 71 Boiling points for five binary systems of sulfolane with aromatic hydrocarbons at 101.33 kpa Yang-Xin Yu, Ming-Yan He, Guang-Hua Gao, Zong-Cheng Li Department of
More informationPrediction of phase equilibria in waterralcoholralkane systems
Fluid Phase Equilibria 158 160 1999 151 163 Prediction of phase equilibria in waterralcoholralkane systems Epaminondas C. Voutsas ), Iakovos V. Yakoumis, Dimitrios P. Tassios Laboratory of Thermodynamics
More informationTHERMODYNAMIC EXCESS PROPERTIES IN BINARY MIXTURES OF MOLECULES OF DIFFERENT SIZES AND SHAPES. Introduction
THERMODYNAMIC EXCESS PROPERTIES IN BINARY MIXTURES OF MOLECULES OF DIFFERENT SIZES AND SHAPES Dana Dragoescu, A. Barhala and Rodica Vilcu Isothermal vapour-liquid equilibrium (VLE) data for binary mixtures
More informationA Generalized Correlation for Pool Boiling Heat Transfer Coefficient Based on Corresponding State Rule for Pure Compounds and Binary Mixtures
A Generalized Correlation for Pool Boiling Heat Transfer Coefficient Based on Corresponding State Rule for Pure Compounds and Binary Mixtures HASAN QABAZARD and MAHMOOD MOSHFEGHIAN 1 Petroleum Research
More informationIsobaric Vapor-Liquid Equilibria of Mesitylene + 1- Heptanol and Mesitylene +1-Octanol at 97.3 kpa
World Academy of Science, Engineering and Technology 7 9 Isobaric Vapor-Liquid Equilibria of Mesitylene + - Heptanol and Mesitylene +-Octanol at 97.3 kpa Seema Kapoor, Sushil K. Kansal, Baljinder K. Gill,
More informationVolumetric Study of the Binary Mixtures Containing a Branched Hexane and an Isomeric Chlorobutane
78 Journal of Applied Solution Chemistry and Modeling, 205, 4, 78-84 Volumetric Study of the Binary Mixtures Containing a Branched Hexane and an Isomeric Chlorobutane Hernando Guerrero, Félix M. Royo and
More informationCORRELATION OF (LIQUID + LIQUID) EQUILIBRIUM OF SYSTEMS INCLUDING IONIC LIQUIDS
Brazilian Journal of Chemical Engineering ISSN 0104-6632 Printed in Brazil www.abeq.org.br/bjche Vol. 24, No. 01, pp. 143-149, January - March, 2007 CORRELATION OF (LIQUID + LIQUID) EQUILIBRIUM OF SYSTEMS
More informationVapour-Liquid Equilibrium for the Binary System Dimethylformamide Ethylene Glycol*
Vapour-Liquid Equilibrium for the Binary System Dimethylformamide Ethylene Glycol* E. GRACZOVÁ** and + J. SUROVÝ Department of Chemical and Biochemical Engineering, Faculty of Chemical and Food Technology,
More informationVapor-liquid equilibria for the binary mixtures of methanol+ cyclopentyl methyl ether (CPME)
Korean J. Chem. Eng., 33(10), 2961-2967 (2016) DOI: 10.1007/s11814-016-0145-z INVITED REVIEW PAPER pissn: 0256-1115 eissn: 1975-7220 Vapor-liquid equilibria for the binary mixtures of methanol+ cyclopentyl
More informationpv m = RT + Bp The simplest equation for calculating fugacity, given an equation of state, is Z=1 + B RT p
Chem 42/523 Chemical hermodynamics Homework Assignment # 5 1. *Assume O 2 gas obeys the virial equation pv m = R + Bp with B = 12.5 cm 3 mol 1 at 298.15 K. Calculate the fugacity of oxygen at p = 1. MPa
More informationA Simple Continuous Mixture Droplet Evaporation Model with Multiple Distribution Functions
Introduction A Simple Continuous Mixture Droplet Evaporation Model with Multiple Distribution Functions William Hallett and Claire Grimwood Dept. of Mechanical Engineering, University of Ottawa, Ottawa,
More informationA Short Method To Calculate Residue Curve Maps in Multireactive and Multicomponent Systems
pubs.acs.org/iecr A Short Method To Calculate Residue Curve Maps in Multireactive and Multicomponent Systems Marcelino Carrera-Rodríguez, Juan Gabriel Segovia-Hernandez,*, and Adrian Bonilla-Petriciolet
More informationPublication V. Reprinted with permission from Elsevier Elsevier Science
Publication V Ouni T., Zaytseva A., Uusi-Kyyny P., Pokki J.-P. and Aittamaa J., Vapour-liquid equilibrium for the 2-methylpropane + methanol, +ethanol, +2-propanol, +2-butanol and +2-methyl-2-propanol
More informationModified Raoult's Law and Excess Gibbs Free Energy
ACTIVITY MODELS 1 Modified Raoult's Law and Excess Gibbs Free Energy Equilibrium criteria: f V i = L f i For vapor phase: f V i = y i i P For liquid phase, we may use an activity coefficient ( i ), giving:
More informationComparison of distillation arrangement for the recovery process of dimethyl sulfoxide
Korean J. Chem. Eng., 24(3), 438-444 (2007) SHORT COMMUNICATION Comparison of distillation arrangement for the recovery process of dimethyl sulfoxide Jungho Cho and Dong Min Kim* Department of Chemical
More informationVOL. 11, NO. 3, FEBRUARY 2016 ISSN
COMPARATIVE ANALYSIS OF EXPERIMENTAL AND NUMERICAL INVESTIGATION ON THERMOPHYSICAL PROPERTIES IN HYDROCARBON MIXTURES USING JOUYBAN-ACREE MODEL AT VARIOUS TEMPERATURES R. Ramesh, T. K. Thanusha, M. Y.
More informationDensities and Viscosities of the Ternary Mixtures Water + Butyl Acetate + Methanol and Water + Ethyl Propionate + Methanol at 303.
926 J. Chem. Eng. Data 2000, 45, 926-931 Densities and Viscosities of the Ternary Mixtures Water + Butyl Acetate + Methanol and Water + Ethyl Propionate + Methanol at 303.15 K Zoran P. Visak, Abel G. M.
More informationTERNARY LIQUID-LIQUID AND MISCIBLE BINARY VAPOR-LIQUID EQUILIBRIUM DATA FOR THE TWO AND WATER ACETONITRILE-ETHYL ACETATE
TERNARY LIQUID-LIQUID AND MISCIBLE BINARY VAPOR-LIQUID EQUILIBRIUM DATA FOR THE TWO SYSTEMS n-hexane ETHANOL ACETONITRILE AND WATER ACETONITRILE-ETHYL ACETATE Hiroshi SUGI and Takashi KATAYAMA Department
More informationGroup contribution methodsðideal tools for the synthesis and design of separation processes*
Pure Appl. Chem., Vol. 71, No. 6, pp. 939±949, 1999. Printed in Great Britain. q 1999 IUPAC Group contribution methodsðideal tools for the synthesis and design of separation processes* JuÈ rgen Gmehling²
More informationFLASH POINT FOR BINARY MIXTURES
Engineering Journal of Qatar University, Vol. 7, 1994, p. 27-36 FLASH POINT FOR BINARY MIXTURES A.B. Donaldson* and Saleh AI-Sharafi** *Visiting Professor in the Department of Chemical Engineering, Qatar
More informationOptimization study on the azeotropic distillation process for isopropyl alcohol dehydration
Korean J. Chem. Eng., 23(1), 1-7 (2006) Optimization study on the azeotropic distillation process for isopropyl alcohol dehydration Jungho Cho and Jong-Ki Jeon*, Department of Chemi Engineering, Dong Yang
More informationPRACTICAL DATA CORRELATION OF FLASHPOINTS OF BINARY MIXTURES BY A RECIPROCAL FUNCTION: THE CONCEPT AND NUMERICAL EXAMPLES
HERMAL SCIENCE, Year 0, Vol. 5, No. 3, pp. 905-90 905 Open forum PRACICAL DAA CORRELAION OF FLASHPOINS OF BINARY MIXURES BY A RECIPROCAL FUNCION: HE CONCEP AND NUMERICAL EXAMPLES by Mariana HRISOVA a,
More informationVapor liquid equilibrium of carbon dioxide with ethyl caproate, ethyl caprylate and ethyl caprate at elevated pressures
J. of Supercritical Fluids 28 (2004) 1 9 Vapor liquid equilibrium of carbon dioxide with ethyl caproate, ethyl caprylate and ethyl caprate at elevated pressures Weng-Hong Hwu, Jaw-Shin Cheng, Kong-Wei
More informationModified solvation model for salt effect on vapor liquid equilibria
Fluid Phase Equilibria 194 197 (2002) 701 715 Modified solvation model for salt effect on vapor liquid equilibria Hideaki Takamatsu, Shuzo Ohe Department of Chemical Engineering, Graduated School of Engineering,
More informationVapor liquid equilibria of carbon dioxide with diethyl oxalate, ethyl laurate, and dibutyl phthalate binary mixtures at elevated pressures
Fluid Phase Equilibria 181 (2001) 1 16 Vapor liquid equilibria of carbon dioxide with diethyl oxalate, ethyl laurate, and dibutyl phthalate binary mixtures at elevated pressures Kong-Wei Cheng, Muoi Tang
More informationChapter 10. Vapor/Liquid Equilibrium: Introduction
Chapter 10 Vapor/Liquid Equilibrium: Introduction Preceding chapters have dealt largely with pure substances or with constant-composition mixtures. e.g., air. However, composition changes are the desired
More informationPhase Separation Degree of Freedom Analysis. Binary Vapor-Liquid Systems. Azeotropic Systems. - Gibbs phase rule F C P 2 -General analysis
Lecture 5. Single Equilibrium Stages (1) Phase Separation [Ch. 4] Degree of Freedom Analysis - Gibbs phase rule F CP2 -General analysis Binary Vapor-Liquid Systems - Examples of binary system - Phase equilibrium
More informationOptimization of the Sulfolane Extraction Plant Based on Modeling and Simulation
Korean J. Chem. Eng., 17(6), 712-718 (2000) Optimization of the Sulfolane Extraction Plant Based on Modeling and Simulation Yu-Jung Choi, Tae-In Kwon and Yeong-Koo Yeo Department of Chemical Engineering,
More informationExcess Heat Capacity Surfaces for Water-Alkanol Mixtures by the UNIQUAC Model
University of Nebraska - Lincoln From the SelectedWorks of YASAR DEMIREL 1995 Excess Heat Capacity Surfaces for Water-Alkanol Mixtures by the UNIQUAC Model YASAR DEMIREL H Paksoy Available at: https://works.bepress.com/yasar_demirel/47/
More informationExperimental and Simulation Study on the Reactive Distillation Process for the Production of Ethyl Acetate
Experimental and Simulation Study on the Reactive Distillation Process for the Production of Ethyl Acetate Jongkee Park, Na-Hyun Lee, So-Jin Park, and Jungho Cho, Separation Process Research Center, Korea
More informationEstimation of Vapour Pressures of Organic Liquids using Group Contributions and Group Interactions
Estimation of Vapour Pressures of Organic Liquids using Group Contributions and Group Interactions B. Moller*, J. Rarey**, D. Ramjugernath* * University of Kwazulu-Natal, Durban 4041, South Africa ** Technische
More informationProblem Appendix Antoine constants Important properties of unordered packings... 22
Contents Sample problems and eercises Distillation... 3 Sample problems... 3 Sample : Calculating vapor phase composition for immiscible liquids... 3 Sample 2: Calculating boiling point and vapor phase
More informationThermophysical Properties of Ethane from Cubic Equations of State
Thermophysical Properties of Ethane from Cubic Equations of State MIHAELA NOUR, DANIELA DUNA, MIRELA IONITA, VIOREL FEROIU *, DAN GEANA Politehnica University Bucharest, Department of Inorganic Chemistry,
More informationLiquid-Liquid Equilibrium for Extraction of Benzene from 1-Hexene Using Two Different Solvents
Scientific Research China Petroleum Processing and Petrochemical Technology 2018, Vol. 20, No. 1, pp 61-66 March 30, 2018 Liquid-Liquid Equilibrium for Extraction of Benzene from 1-Hexene Using Two Different
More informationOverall: 75 ECTS: 7.0
Course: Chemical Engineering Thermodynamics Language: English Lecturer: Prof. dr. sc. Marko Rogošić TEACHING WEEKLY SEMESTER Lectures 3 45 Laboratory 1 15 Seminar 1 15 Overall: 75 ECTS: 7.0 PURPOSE: Within
More informationEXTRACTIVE DISTILLATION OF ETHYLBENZENE AND STYRENE USING SULFOLANE AS SOLVENT: LOW PRESSURE ISOBARIC VLE DATA
Distillation Absorption 2010 A.B. de Haan, H. Kooman and A. Górak (Editors) All rights reserved by authors as per DA2010 copyright notice EXTRACTIVE DISTILLATION OF ETHYLBENZENE AND STYRENE USING SULFOLANE
More informationTHERMODYNAMIC CONSISTENCY TESTS FOR PHASE EQUILIBRIUM IN LIQUID SOLUTE+SUPERCRITICAL SOLVENT MIXTURES
THERMODYNAMIC CONSISTENCY TESTS FOR PHASE EQUILIBRIUM IN LIQUID SOLUTE+SUPERCRITICAL SOLVENT MIXTURES José O. Valderrama 1, and Víctor H. Alvarez 1 Fac. de Ingeniería, Depto. Ing. Mecánica, Univ. de la
More informationON THE APPLICABILITY OF THE UNIQUAC METHOD TO TERNARY LIQUID - LIQUID EQUILIBRIA
C2,3 The Journal - cyclic of carbonates the Argentine derived Chemical from Society uridine - and Vol. inosine 92 - Nº 4/6, 81-90 (2004) 81 ON THE APPLICABILITY OF THE UNIQUAC METHOD TO TERNARY LIQUID
More informationMEASUREMENT AND PREDICTION OF FUEL OXYGENATES MIXTURES EXCESS THERMOPHYSICAL PROPERTIES - A REVIEW
MEASUREMENT AND PREDICTION OF FUEL OXYGENATES MIXTURES EXCESS THERMOPHYSICAL PROPERTIES - A REVIEW T. K. Thanusha, R. Ramesh, A. S. Noor Asma Fazli, M. Y. M. Yunus and K. Ramesh Faculty of Chemical & Natural
More informationCalculations of thermodynamic derivative properties from the NRTL and UNIQUAC models
University of Nebraska - Lincoln From the SelectedWorks of YASAR DEMREL 1997 Calculations of thermodynamic derivative properties from the NRTL and UNQUAC models YASAR DEMREL Available at: https://works.bepress.com/yasar_demirel/61/
More informationMolecular Interaction Study of Binary Solutions of n-butyl Acetate and Isopropanol at Various Temperatures
Research Inventy: International Journal of Engineering And Science Vol.8, Issue 2 (May 2018), PP -54-59 Issn (e): 2278-4721, Issn (p):2319-6483, www.researchinventy.com Molecular Interaction Study of Binary
More informationIsobaric Vapour-Liquid Equilibrium of Binary Mixture of 1, 2-Di-chloroethane with 1-Heptanol at Kpa
Isobaric Vapour-Liquid Equilibrium of Binary Mixture of 1, 2-Di-chloroethane with 1-Heptanol at 95.72 Kpa Sai kumar Bitta Department Of Chemical Engineering Chaitanya Bharathi Institute of Technology Guide:
More informationThe successes and limitations of this thermodynamic model in predicting the solubility of organic solutes in pure solvents
PC-SAFT The successes and limitations of this thermodynamic model in predicting the solubility of organic solutes in pure solvents Gross and Sadowski s (21) modified SAFT, perturbed chain SAFT, was studied
More informationVapor liquid equilibria of carbon dioxide with ethyl benzoate, diethyl succinate and isoamyl acetate binary mixtures at elevated pressures
Journal of Supercritical Fluids 21 (2001) 111 121 wwwelseviercom/locate/supflu Vapor liquid equilibria of carbon dioxide with ethyl benzoate, diethyl succinate and isoamyl acetate binary mixtures at elevated
More informationExperimental Investigation of Excess molar enthalpies of binary mixtures formed by ethyl acetate (with Cyclohexane or 1-Butanol or 1- Hexene)
Experimental Investigation of Excess molar enthalpies of binary mixtures formed by ethyl acetate (with Cyclohexane or 1-Butanol or 1- Hexene) Mahendra V. Guddad 1*, K. L. Shivabasappa 2, Bhausaheb L. Pangarkar
More informationContinuous Thermodynamics of Petroleum Fluids Fractions
Chemical Engineering and Processing Volume 40, Issue 5, Pages 431 435, 2001 DOI: 10.1016/S0255-2701(00)00140-9 Print ISSN: 02552701 G.Reza Vakili-Nezhaad a, Hamid Modarress b, G.Ali Mansoori c a Uniersity
More informationCHAPTER 3 EXPERIMENTAL SET UP AND PROCEDURE
16 CHAPTER 3 EXPERIMENTAL SET UP AND PROCEDURE 3.1 DETERMINATION OF VAPOUR LIQUID EQUILIBRIA Iso baric vapor liquid equilibria data have been obtained, using a Smith and Bonner (1949) type still, a modified
More information~ K 에서 2- 브로모프로판 - 메탄올이성분혼합물의밀도, 점성도, 여분성질
Journal of the Korean Chemical Society 00, Vol. 54, No. Printed in the Republic of Korea DOI 0.50/jkcs.00.54.0.07 98.5 ~ 38.5 K 에서 - 브로모프로판 - 메탄올이성분혼합물의밀도, 점성도, 여분성질 Hua Li*, Zhen Zhang, and Lei Zhao School
More informationIlE. Simulation of a Distillation Column on an IBM PC, Accounting for Real Behaviour of Electrolyte Solutions * c I
~~ Chem. Eng. Technol. 14 (1991) 295-300 295 Simulation of a Distillation Column on an IBM PC, Accounting for Real Behaviour of Electrolyte Solutions * Andre Bosen and Manfred Roth** This contribution
More informationKolmetz Handbook of Process Equipment Design BTX EXTRACTION UNIT DESIGN, SIZING AND TROUBLESHOOTING (ENGINEERING DESIGN GUIDELINE)
Page : 1 of 75 KLM Technology #03-12 Block Aronia, Jalan Sri Perkasa 2 Taman Tampoi Utama 81200 Johor Bahru SOLUTIONS, STANDARDS AND SOFTWARE www.klmtechgroup.com Rev 01- March 2017 Co Author: Rev 01 Yulis
More informationDETERMINATION OF OPTIMAL ENERGY EFFICIENT SEPARATION SCHEMES BASED ON DRIVING FORCES
DETERMINATION OF OPTIMAL ENERGY EFFICIENT SEPARATION SCHEMES BASED ON DRIVING FORCES Abstract Erik Bek-Pedersen, Rafiqul Gani CAPEC, Department of Chemical Engineering, Technical University of Denmark,
More informationSITARAM K. CHAVAN * and MADHURI N. HEMADE ABSTRACT INTRODUCTION
Int. J. Chem. Sci.: 11(1), 013, 619-67 ISSN 097-768X www.sadgurupublications.com DENSITIES, VISCOSITIES AND EXCESS THERMODYNAMIC PROPERTIES OF MONOMETHYL AMMONIUM CHLORIDE IN TETRAHYDROFURAN AND WATER
More information* Institut FranGais du PCtrole, 1 et 4 avenue de Bois PrCau, BP 311, Rueil-
Pure &App/. Chem., Vol. 67, No. 6, pp. 985-992, 1995. Printed in Great Britain. Q 1995 IUPAC Separation of alcohol/ether/hydrocarbon mixtures in industrial etherification processes for gasoline production
More informationVOL. 11, NO. 3, FEBRUARY 2016 ISSN
EXPERIMENTAL AND NUMERICAL INVESTIGATION ON THERMOPHYSICAL PROPERTIES OF HYDROCARBON LIQUID MIXTURES USING KRISHNAN-LADDHA AND JOUYBAN-ACREE MODELS AT VARIOUS TEMPERATURES R. Ramesh, T. K. Thanusha, M.
More informationDevelopment new correlations for NRTL Parameters in Polymer Solutions
Rhodes, Greece, August 0-, 008 Development new correlations for NRTL Parameters in Polymer Solutions A. Saatchi, M. Edalat* Oil and Gas Center of Excellence, Department of Chemical Engineering University
More informationA Sequential and Hierarchical Approach for the Feasibility Analysis and the Preliminary Synthesis and Design of Reactive Distillation Processes
A Sequential and Hierarchical Approach for the Feasibility Analysis and the Preliminary Synthesis and Design of Reactive Distillation Processes Raphaële Thery, Xuân-Mi Meyer 1, Xavier Joulia Laboratoire
More informationSOLUBILITY OF CO 2 IN BRANCHED ALKANES IN ORDER TO EXTEND THE PPR78 MODEL TO SUCH SYSTEMS
SOLUBILITY OF CO IN BRANCHED ALKANES IN ORDER TO EXTEND THE PPR78 MODEL TO SUCH SYSTEMS Fabrice MUTELET, Stéphane VITU and Jean-Noël JAUBERT (*) Institut National Polytechnique de Lorraine, Ecole Nationale
More informationChapter 2 Equilibria, Bubble Points, Dewpoints, Flash Calculations, and Activity Coefficients
Chapter 2 Equilibria, Bubble Points, Dewpoints, Flash Calculations, and Activity Coefficients 2.1 Vapour Pressure Calculations The basis for all phase equilibrium calculations are the vapour pressures
More informationMixing properties of propyl acetate+aromatic hydrocarbons at K
Korean J. Chem. Eng., 23(1), 93-101 (2006) Mixing properties of propyl acetate+aromatic hydrocarbons at 298.15 K José M. Resa, Cristina González, Soraya Prieto, Elena Díez and Miguel Iglesias Dpto. de
More informationEXTRACTION OF DECANE AND HEXANE WITH SUPERCRITICAL PROPANE: EXPERIMENTS AND MODELING
International Journal of Chemical & Petrochemical Technology (IJCPT) ISSN 2277-4807 Vol. 3, Issue 2, Jun 2013, 71-82 TJPRC Pvt. Ltd. EXTRACTION OF DECANE AND HEXANE WITH SUPERCRITICAL PROPANE: EXPERIMENTS
More informationLiquid liquid equilibria of aqueous mixtures containing selected dibasic esters and/or methanol
Fluid Phase Equilibria 248 (2006) 174 180 Liquid liquid equilibria of aqueous mixtures containing selected dibasic esters and/or methanol Shih-Bo Hung a, Ho-Mu Lin a, Cheng-Ching Yu b, Hsiao-Ping Huang
More informationImprovement of separation process of synthesizing MIBK by the isopropanol one-step method
Korean J. Chem. Eng., 23(2), 264-270 (2006) SHORT COMMUNICATION Improvement of separation process of synthesizing MIBK by the isopropanol one-step method Zhigang Lei, Jianwei Li, Chengyue Li and Biaohua
More informationAn augmented hard core equation of state generalized in terms of T,, P, and o
Pure&App/. Chern., Vol. 61, No. 8, pp. 1413-1418, 1989. Printed in Great Britain. 0 1989 IUPAC An augmented hard core equation of state generalized in terms of T,, P, and o 1 2 Hasan Orbey and Juan H.
More informationVapor-liquid equilibrium
Vapor-liquid equilibrium From Wikipedia, the free encyclopedia Vapor-liquid equilibrium, abbreviated as VLE by some, is a condition where a liquid and its vapor (gas phase) are in equilibrium with each
More informationComputer Aided Identification of Acetone and Chloroform Mixture Behavior
Computer Aided Identification of Acetone and Chloroform Mixture Behavior Sarah Torkamani Chemical Engineering PhD Student Department of Chemical and Petroleum Engineering, Sharif University of Technology,
More informationThermally Coupled Distillation Systems: Study of an Energy-efficient Reactive Case
F. O. BARROSO-MUÑOZ et al., Thermally Coupled Distillation Systems: Study of, Chem. Biochem. Eng. Q. 21 (2) 115 120 (2007) 115 Thermally Coupled Distillation Systems: Study of an Energy-efficient Reactive
More informationJ. Reyes, A. Gómez & A. Marcilla Dpto. Ingeniería Química, Universidad de Alicante, Apdo. de Correos nº 99, Alicante 03080, España.
MULTICOMPONENT RECTIFICATION: A NEW METHOD OF CALCULATION J. Reyes, A. Gómez & A. Marcilla Dpto. Ingeniería Química, Universidad de Alicante, Apdo. de Correos nº 99, Alicante 03080, España. This poster
More informationRapid Measurements of Thermodynamic Properties for Alternative Refrigerants with Vibrating-Tube
Rapid Measurements of Thermodynamic Properties for Alternative Refrigerants with Vibrating-Tube Densimeter Fifteenth Symposium on Thermophysical Properties Y. Kano : speaker M. Hasumoto Y. Kayukawa K.
More informationBatch extractive distillation of mixture methanol-acetonitrile using aniline as a asolvent
48 Pol. J. Chem. Polish Tech., Journal Vol. 14, of No. Chemical 3, 2012 Technology, 14, 3, 48 53, 10.2478/v10026-012-0083-4 Batch extractive distillation of mixture methanol-acetonitrile using aniline
More informationInvestigation of benzene and cycloparaffin containing hexane fractions skeletal isomerization on Pt/sulphated metal-oxide catalyst
Investigation of benzene and cycloparaffin containing hexane fractions skeletal isomerization on Pt/sulphated metal-oxide catalyst Zsolt Szoboszlai*, Jenő Hancsók* *University of Pannonia, Institute of
More informationPrediction of surface tension of binary mixtures with the parachor method
Prediction of surface tension of binary mixtures with the parachor method Tomáš Němec 1,a Institute of Thermomechanics ASCR, v.v.i., Dolejškova, 18 Praha 8, Czech Republic Abstract. The parachor method
More informationThermodynamic Properties of Refrigerant R116 from Cubic Equations of State
Thermodynamic Properties of Refrigerant R116 from Cubic Equations of State DANIELA DUNA, MIRELA IONITA, VIOREL FEROIU *, DAN GEANA Politehnica University Bucharest, Department of Applied Physical Chemistry
More informationASIAN JOURNAL OF CHEMISTRY
Asian Journal of Chemistry; Vol., No. (14), 79-779 ASIAN JOURNAL OF CHEMISTRY http://dx.doi.org/1.1433/ajchem.14.1741 Experimental Study of Vapor-Liquid Equilibrium and Optimization of Pressure-Swing Distillation
More informationA NEW AND A SIMPLE MODEL FOR SURFACE TENSION PREDICTION OF WATER AND ORGANIC LIQUID MIXTURES * R. TAHERY AND H. MODARRESS **
Iranian Journal of Science & Technology, Transaction B, Engineering, Vol. 29, No. B5 Printed in The Islamic Republic of Iran, 25 Shiraz University NE ND SIMPLE MODEL FOR SURFCE TENSION PREDICTION OF TER
More informationSOFTWARE INTELIGENT PACKAGE FOR PHASE EQULIBRIA (PHEQ) IN SYSTEMS APPLIED IN CHEMISTRY AND CHEMICAL ENGINEERING
SOFTWARE INTELIGENT PACKAGE FOR PHASE EQULIBRIA (PHEQ) IN SYSTEMS APPLIED IN CHEMISTRY AND CHEMICAL ENGINEERING Prof. Dr. Dan GEANĂ University Politechnica Bucharest Abstract The importance and role of
More informationCHEM Exam 2 - October 11, INFORMATION PAGE (Use for reference and for scratch paper)
CHEM 5200 - Exam 2 - October 11, 2018 INFORMATION PAGE (Use for reference and for scratch paper) Constants and Conversion Factors: R = 0.082 L-atm/mol-K = 8.31 J/mol-K = 8.31 kpa-l/mol-k 1 L-atm = 101
More informationREV. CHIM. (Bucureºti) 58 Nr
1069 High-Pressure Vapour-Liquid Equilibria of Carbon Dioxide + 1-Pentanol System Experimental Measurements and Modelling CATINCA SECUIANU*, VIOREL FEROIU, DAN GEANÃ Politehnica University Bucharest, Department
More informationExcess Molar Volume and Viscosity Study of Ternary Mixtures of tert-butylmethylether and n-heptane with Alcohols at K
Excess Molar Volume and Viscosity Study of Ternary Mixtures of tert-butylmethylether and n-heptane with Alcohols at 293.15 K MARIA MAGDALENA BUDEANU*, VASILE DUMITRESCU, OCTAV PANTEA Petroleum and Gas
More informationIsobaric vapor-liquid equilibrium for methanol+benzene+1-octyl-3-methylimidazolium tetrafluoroborate
Korean J. Chem. Eng., 29(7), 941-945 (2012) DOI: 10.1007/s11814-011-0262-7 INVITED REVIEW PAPER Isobaric vapor-liquid equilibrium for methanol+benzene+1-octyl-3-methylimidazolium tetrafluoroborate Qunsheng
More information,, Seong-Bo Kim,Hai-SongBae, and Jeong-Sik Han
Jungho Cho, So-Jin Park,, Myung-Jae Choi,, Seong-Bo Kim,Hai-SongBae, and Jeong-Sik Han Department of Chemical Engineering, Dong-Yang University, Kyoungbuk, 750-711, Korea *Department of Chemical Engineering,
More informationSolving mass transfer problems on the computer using Mathcad
Solving mass transfer problems on the computer using Mathcad E. N. Bart, J. Kisutcza NJIT, Department of Chemical Engineering, University Heights, Newark NJ 712-1982 Tel 973 596 2998, e-mail: Bart@NJIT.edu
More informationExcess Molar Enthalpies of Binary and Ternary Systems Involving Hydrocarbons and Ethers
Excess Molar Enthalpies of Binary and Ternary Systems Involving Hydrocarbons and Ethers A Thesis Submitted to the College of Graduate Studies and Research in Partial Fulfillment of the Requirements for
More informationPHASE EQUILIBRIUM INVESTIGATION OF THE WATER AND ACETONITRILE SOLVENT WITH HEAVY HYDROCARBONS
PHASE EQUILIBRIUM INVESTIGATION OF THE WATER AND ACETONITRILE SOLVENT WITH HEAVY HYDROCARBONS by CALEB NARASIGADU [BSc. (Eng)] University of KwaZulu Natal Submitted in fulfillment of the academic requirements
More informationMeasurement and Calculation of Physico-Chemical Properties of Binary Mixtures Containing Xylene and 1- Alkanol
Chemical Methodologies 2(2018) 308-314 Chemical Methodologies Journal homepage: http://chemmethod.com Original Research article Measurement and Calculation of Physico-Chemical Properties of Binary Mixtures
More informationAPPLICATION NOTE. A Capillary Approach to ASTM D3606: Test Method for Determination of Benzene and Toluene in Finished Motor and Aviation Gasoline
A Capillary Approach to ASTM D3606: Test Method for Determination of Benzene and Toluene in Finished Motor and Aviation Gasoline Fast : Cycles in
More informationFinding Rigorous Thermodynamic Model parameters for the Simulation of a Reactive Distillation Column: Case of ETBE Production
Finding Rigorous Thermodynamic Model parameters for the Simulation of a Reactive Distillation Column: Case of ETBE Production Gisela N. Durruty, M. Soledad Diaz, Patricia M. Hoch * Universidad Nacional
More informationPractice Examinations Chem 393 Fall 2005 Time 1 hr 15 min for each set.
Practice Examinations Chem 393 Fall 2005 Time 1 hr 15 min for each set. The symbols used here are as discussed in the class. Use scratch paper as needed. Do not give more than one answer for any question.
More informationNote: items marked with * you should be able to perform on a closed book exam. Chapter 10 Learning Objective Checklist
Note: items marked with * you should be able to perform on a closed book exam. Chapter 10 Learning Objective Checklist Sections 10.1-10.13 find pure component properties on a binary P-x-y or T-x-y diagram.*
More informationPHASE EQUILIBRIUM CALCULATIONS OF HIGHLY POLAR SYSTEMS
Fluid Phase Equilibria Journal Volume 32, Pages 139-149, 1987 139 PHASE EQUILIBRIUM CALCULATIONS OF HIGHLY POLAR SYSTEMS El-HOUARI BENMEKKI and G.ALI MANSOORI* Department of Chemical Engineering, University
More information