New apparatus to perform fast determinations of mixture vapor–liquid equilibria up to 10 MPa and 423 K

Laugier, Serge; Richon, Dominique

doi:10.1063/1.1138909

Cited by 104 publications

(55 citation statements)

References 11 publications

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“…The principle of the apparatus is similar to that described by Laugier and Richon. 9 The apparatus has been described in our previous works. 2,3,10 In brief, the apparatus consists of a stainless steel equilibrium cell (approximately 40 cm 3 ) with two sapphire viewing windows and a movable ROLSI which was used to individually withdraw samples of the liquid and vapor phases at equilibrium.…”

Section: Methodsmentioning

confidence: 99%

Isothermal Vapor–Liquid Equilibrium Data for the 1,1,2,3,3,3-Hexafluoroprop-1-ene +1,1,2,2,3,3,4,4-Octafluorocyclobutane Binary System: Measurement and Modeling from (292 to 352) K and Pressures up to 2.6 MPa

et al. 2015

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Isothermal vapor−liquid equilibrium data are presented for the 1,1,2,3,3,3-hexafluoroprop-1-ene and 1,1,2,2,3,3,4,4-octafluorocyclobutane binary system at (292.89, 323.02 and 352.71) K, with pressures ranging from (0.3 to 2.6) MPa. The data were measured using an apparatus based on the "staticanalytic" method, equipped with a single movable rapid online sampler-injector (ROLSI). The expanded uncertainties are estimated at 0.11 K, 4 kPa, 0.010 and 0.007 for the temperature, pressure, and the equilibrium liquid and vapor mole fractions, respectively. The experimental vapor−liquid equilibrium data were correlated using the Peng−Robinson equation of state with the Mathias −Copeman alpha function. The model provides a satisfactory description of the experimental data.

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Section: Methodsmentioning

confidence: 99%

Isothermal Vapor–Liquid Equilibrium Data for the 1,1,2,3,3,3-Hexafluoroprop-1-ene +1,1,2,2,3,3,4,4-Octafluorocyclobutane Binary System: Measurement and Modeling from (292 to 352) K and Pressures up to 2.6 MPa

et al. 2015

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“…This leaves 3 adjustable parameters in the PR-MC-WS-NRTL model: k 12 , τ 12 and τ 21 . These parameters are assumed to be temperature dependent.…”

Section: Peng-robinson Eosmentioning

confidence: 99%

“…The vapor phase sampling capillary inlet was placed close to the top flange inside the cell, while the liquid phase capillary inlet could be moved vertically inside the cell to be at an appropriate position in the liquid phase. The use of these Rolsi TM samplers for VLE measurements was first described in [21].…”

Section: Description Of Setupmentioning

confidence: 99%

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Vapor–liquid equilibrium data for the carbon dioxide and nitrogen (CO2 + N2) system at the temperatures 223, 270, 298 and 303 K and pressures up to 18 MPa

Westman

Stang

Løvseth

et al. 2016

Fluid Phase Equilibria

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A new setup for the measurement of vapor-liquid phase equilibria of CO 2 -rich mixtures relevant for carbon capture and storage (CCS) transport conditions is presented. An isothermal analytical method with a variable volume cell is used. The apparatus is capable of highly accurate measurements in terms of pressure, temperature and composition, also in the critical region. Vapor-liquid equilibrium (VLE) measurements for the binary system CO 2 +N 2 are reported at 223, 270, 298 and 303 K, with estimated standard uncertainties of maximum 0.006 K in the temperature, maximum 0.003 MPa in the pressure, and maximum 0.0004 in the mole fractions of the phases. These measurements are verified against existing data. Although some data exists, there is little trustworthy data around critical conditions, and our data indicate a need to revise the parameters of existing models. A fit made against our data of the vapor-liquid equilibrium prediction of GERG-2008/EOS-CG for CO 2 +N 2 is presented. At 223 and 298 K, the critical region of the isotherm are fitted using a scaling law, and high accuracy estimates for the critical composition and pressure are found.

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“…Among a few notable studies, Connolly (1 962) measured vapro-liquid equilibria (VLE) for hydrogen/benzene mixtures with a static apparatus over the temperatures of 430-530 K and the pressures of 2-18 MPa, while Grayson and Streed (1963) used a flow apparatus to determine VLE of hydrogen/gas oils at temperatures up to 750 K and pressures to 20 MPa. Renon and coworkers at Ecole des Mines de Paris Laugier et al, 1983Laugier et al, ,1986Cohen and Richon, 1986) have developed various apparatus for high-pressure VLE measurements at elevated temperatures. Other apparatus, which have been constructed in recent years essentially for mixtures of interest in coal conversion processes, include those of Prather et al (1977), Simnick et al (1977), Nasir et al (1980), Wilson et al (1981), Sung (1981), Harrison et al (1982Harrison et al ( , 1985, Linet al (1989, Ramanujan et al (1989, Ding et al (1989, Inomata et al (1986, and Thies and coworkers (Theis andPaulaities, 1984, 1986;Thies et al, 1988).…”

mentioning

confidence: 99%

Flow apparatus for phase equilibrium measurement at elevated temperatures

Lin

1990

AIChE Journal

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A flow apparatus was developed to determine phase equilibria at elevated temperatures and pressures. The key component of the apparatus is a high-pressure view cell equipped with transparent sapphire windows for visual observation of the liquid level. The flow apparatus is used to the best advantage when the residence time of chemicals (or bic-materials) in the high-temperature zone has to be minimized to eliminate the possibility of thermal decomposition or polymerization reactions. Because the technique has the advantages of rapid attainment of equilibrium conditions and straightforward sampling procedures, it produces a fairly large quantity of data with a minimum amount of time. The sample system also offers the option of taking a desired size of sample by controlling the length of sampling time. This is important particularly for the asymmetric mixtures of a light gas in a very heavy compound of low volatility at some extreme conditions, for which a sufficiently large amount of samples are needed to determine the phase compositions with reasonable accuracy. The flow apparatus of different designs have been used for measurements of vapor-liquid and liquid-liquid equilibria for years. However, it is difficult for multiphase mixtures, and the liquid feed pump cannot handle solids of high-melting points.In operation of a flow apparatus, the liquid level in the equilibrium cell must be sensed and controlled at a certain range of elevation. Simnick et al. (1977) designed a blind cell in which an electric capacitor was installed to detect the liquid level. A similar cell was later fabricated by Inomata and coworkers (1986). However, the capacitor fails to function properly for the mixtures which are electrically conductive (Lin et al., 1985(Lin et al., , 1986. Lin and coworkers (1985) developed a visual cell in which a transparent sapphire window was equipped at each end of the cell body to permit observation of liquid level. A modification of this cell with a new design to improve its sealing of the sapphire windows for operation at higher pressures is Corrapondcna concerning thic pper ahould be addrtsscd to H. hi. Lin.

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New apparatus to perform fast determinations of mixture vapor–liquid equilibria up to 10 MPa and 423 K

Cited by 104 publications

References 11 publications

Isothermal Vapor–Liquid Equilibrium Data for the 1,1,2,3,3,3-Hexafluoroprop-1-ene +1,1,2,2,3,3,4,4-Octafluorocyclobutane Binary System: Measurement and Modeling from (292 to 352) K and Pressures up to 2.6 MPa

Isothermal Vapor–Liquid Equilibrium Data for the 1,1,2,3,3,3-Hexafluoroprop-1-ene +1,1,2,2,3,3,4,4-Octafluorocyclobutane Binary System: Measurement and Modeling from (292 to 352) K and Pressures up to 2.6 MPa

Vapor–liquid equilibrium data for the carbon dioxide and nitrogen (CO2 + N2) system at the temperatures 223, 270, 298 and 303 K and pressures up to 18 MPa

Flow apparatus for phase equilibrium measurement at elevated temperatures

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