Phase equilibriums in the hydrocarbon systems. Phase behavior in the methane-propane-n-butane system

Wiese, Holger; Jacobs, Joan.; Sage, B. H.

doi:10.1021/je60044a021

Cited by 54 publications

(15 citation statements)

References 8 publications

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“…CH 4 -C 2 H 6 system Gomes de Azevedo and Calado (1989) 90-104 0.03-0.51 15 Wichterle and Kobayashi (1972a) 130-200 0.01-52 135 Davalos et al (1976) 250 13-66 8 Gupta et al (1980) 260-280 17-71 52 Wei et al (1995) 210-270 3-65 54 CH 4 -C 3 H 8 system Wichterle and Kobayashi (1972b) 130-213 2-65 105 Reamer et al (1950) 277-361 7-102 128 Akers et al (1954) 158-273 3-100 81 Sage et al (1934) 293-363 10-96 55 CH 4 -nC 4 H 10 system Sage et al (1940) 294-394 2-132 124 Roberts et al (1962) 211-411 2-132 83 Wiese et al (1970) 278-378 14-133 25 Chen et al (1974) 144-278 1-129 173 Kahre (1974) 166-283 1-110 71 CH 4 -CO 2 system Donnelly and Katz (1954) 200-271 11-79 110 Kaminishi et al (1968) 233-273 37-82 14 Arai et al (1971) 253-288 26-85 28 Davalos et al (1976) 230-270 9-86 34 Mraw et al (1978) 153-219 7-65 51 Neumann and Walch (1968) 173-220 27-69 64 Al-Sahhaf et al (1983) 219-270 9-84 32 Xu et al (1992) 288-293 57-82 21 Wei et al (1995) 230-270 11-84 49 H 2 O-CH 4 system at temperatures between 600 and 647.2 K (the critical temperature of water), but it is beyond the scope of this paper. Among the experimental data for the vapor-liquid equilibria of the H 2 O-C 2 H 6 system, the ethane solubility data measured by and the water content data measured by Reamer et al (1943) and Yarrison et al (2006) cover larger P-T range.…”

Section: T (K) P (Bar) Numbermentioning

confidence: 99%

Calculation of vapor–liquid equilibrium and PVTx properties of geological fluid system with SAFT-LJ EOS including multi-polar contribution. Part III. Extension to water–light hydrocarbons systems

Sun

Lai

Dubessy

2014

Geochimica et Cosmochimica Acta

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Section: T (K) P (Bar) Numbermentioning

confidence: 99%

Calculation of vapor–liquid equilibrium and PVTx properties of geological fluid system with SAFT-LJ EOS including multi-polar contribution. Part III. Extension to water–light hydrocarbons systems

Sun

Lai

Dubessy

2014

Geochimica et Cosmochimica Acta

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“…Too high critical pressures of the same authors [10,14,15] were also reported for the systems CO 2 (1) + n-butane (2) and propane (1) + n-butane (2). These authors measured the pressure as a function of volume at a given temperature and composition whereby they obtain the dew and bubble points from the evaluation of the P-V curves.…”

Section: Resultsmentioning

confidence: 67%

“…Niesen and Rainwater [7], whose results agree with the results of this work, already pointed out that in the estimation of critical points from vapor-liquid equilibrium data Reamer et al were guided by the data from Poettmann and Katz. Too high critical pressures of the same authors [10,14,15] were also reported for the systems CO 2 (1) + n-butane (2) and propane (1) + n-butane (2). These authors measured the pressure as a function of volume at a given temperature and composition whereby they obtain the dew and bubble points from the evaluation of the P-V curves.…”

Section: Resultsmentioning

confidence: 90%

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Experimental Determination of Critical Points of Pure Components and Binary Mixtures Using a Flow Apparatus

Horstmann

Fischer

Gmehling³

1999

Chem. Eng. Technol.

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Equations of state can be successfully employed for the description of the phase equilibrium behavior of multicomponent mixtures using binary data alone. Especially in the vicinity of the critical point often only a limited number of phase equilibrium data or data of low quality are available. Critical points of mixtures provide additional information about the location and border of the two-phase region. The PSRK model (Predictive Soave-Redlich-Kwong) [1] combines the SRK equation of state with the group contribution model UNIFAC by the PSRK mixing rule. For the extension of the range of applicability and the improvement of the results of PSRK or other group contribution equations of state the systematic measurement of data required for the fitting of the group interaction parameters is desired. In addition to phase equilibrium data also critical data are of great importance. For this reason a new flow apparatus for the measurement of critical data of pure components and mixtures was developed, which can be operated at temperatures between 280 and 470 K and pressures up to 35 MPa.A common approach for the determination of critical points of mixtures in closed systems is the isothermal or isobaric method connected with an analysis of the gas and liquid phases for the determination of the two-phase region ending at the critical point. Another usual method is the visual detection of critical points where the temperature is varied until the phase border disappears while the temperature increases, or the meniscus reappears while the temperature decreases. The corresponding pressure automatically results from the phase equilibrium pressure. A prerequisite for the measurement of critical points is the exact adjustment of the critical density which requires a variable volume cell.A flow apparatus for the measurement of critical properties of pure components was introduced by Rosenthal and Teja [2]. The variation of density in this apparatus is enabled with the help of a regulation valve at the outlet of the optical cell. Because of the flow mode short retention times are achieved. That is why this technique also allows the determination of critical points of components which show a thermal decomposition. The critical data are determined at different flow rates. Extrapolation of these data to the retention time t = 0 allows the determination of the critical data of such unstable components.The apparatus developed in this study also works in a flow mode and is applicable for pure components as well as binary and multicomponent mixtures. An advantage of this approach is that phase equilibrium is reached before the substances enter the cell. Moreover, the content of the cell is pushed aside so that cleaning and controlled filling of the cell is not necessary. Unfortunately, the critical volume cannot be determined and quite large amounts of substances are needed. Principle of MeasurementA schematic diagram of the apparatus is shown in Fig. 1. Two thermostatted chromatography syringe pumps (Model 260D, ISO) in which the pure...

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“…VLE of ternary methane (1)-propane (2)-butane (3) at 344.26 K. Symbols represent experimental data[67].…”

mentioning

confidence: 99%

Simplified Flory-dimer equation of state for application to non-associating fluids, polymers and their mixtures

Yang

Bae

2015

Fluid Phase Equilibria

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Phase equilibriums in the hydrocarbon systems. Phase behavior in the methane-propane-n-butane system

Abstract: Paris and Virginia Berry were responsible for the reduction of the experimental results to a form suitable for publication.

Cited by 54 publications

References 8 publications

Calculation of vapor–liquid equilibrium and PVTx properties of geological fluid system with SAFT-LJ EOS including multi-polar contribution. Part III. Extension to water–light hydrocarbons systems

Calculation of vapor–liquid equilibrium and PVTx properties of geological fluid system with SAFT-LJ EOS including multi-polar contribution. Part III. Extension to water–light hydrocarbons systems

Experimental Determination of Critical Points of Pure Components and Binary Mixtures Using a Flow Apparatus

Simplified Flory-dimer equation of state for application to non-associating fluids, polymers and their mixtures

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