High-pressure phase behaviour of the binary system {CO2+cis-decalin} from (292.75 to 373.75)K

Vitu, Stéphane; Jaubert, Jean‐Noël; Pauly, Jérôme; Daridon, Jean-Luc

doi:10.1016/j.jct.2008.05.008

Cited by 17 publications

(21 citation statements)

References 28 publications

(52 reference statements)

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“…However, the model was much less successful when CO2 was introduced, mainly at high pressures in the critical and dew regions. This suggests that at least some of the binary parameters involving CO2 are not well predicted by the model of Jaubert and coworkers [28,[38][39][40][41][42][43][44] for T ≥ 323.15 K. In our opinion, this problem is most significant for the (CO2 + CH4) system because no binary VLE data exist for that mixture at temperatures above the critical temperature of CO2 and hence the group parameters between these components were not constrained by experimental data at higher temperatures. The good agreement seen in Figure 5 for the (CO2 + heptane) system lends weight to the idea that it is the interactions between CO2 and the lightest components that need to be adjusted.…”

Section: Evaluation Of the Critical Propertiesmentioning

confidence: 88%

“…The predictive models considered in this work use the group-contribution approach of Jaubert and coworkers [28,[38][39][40][41][42][43][44] to achieve this. In this method, the binary interaction parameter kij is given by …”

Section: Ppr78 and Pr2srkmentioning

confidence: 99%

“…However, in their standard form, these models still require determination of a temperature-dependent interaction parameter for each possible binary combination of the mixture components. Recently, Jaubert and coworkers developed a group contribution method allowing the estimation of the temperature-dependent binary interaction parameters kij(T) in the PR EoS, thereby creating a predictive model that they designated PPR78 [28,[38][39][40][41][42][43][44]. To date, 21 functional groups have been defined including those necessary to describe alkanes, aromatics, naphthenic components as well as light gases such as CO2 and CH4.…”

Section: Introductionmentioning

confidence: 99%

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Experimental and modeling study of the phase behavior of synthetic crude oil+CO2

Ghafri

Maitland

Trusler

2014

Fluid Phase Equilibria

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A full understanding of the phase behavior of CO2-hydrocarbon mixtures at reservoir conditions is essential for the proper design, construction and operation of carbon capture and storage (CCS) and enhanced oil recovery (EOR) processes. While equilibrium data for binary CO2-hydrocarbon mixtures are plentiful, equilibrium data and validated equations of state having reasonable predictive capability for multi-component CO2-hydrocarbon mixtures are limited. In this work, a new synthetic apparatus was constructed to measure the phase behavior of systems containing CO2 and multicomponent hydrocarbons at reservoir temperatures and pressures. The apparatus consisted of a thermostated variable-volume view cell driven by a computer-controlled servo motor system, and equipped with a sapphire window for visual observation. Two calibrated syringe pumps were used for quantitative fluid injection. The maximum operating pressure and temperature were 40 MPa and 473.15 K, respectively. The apparatus was validated by means of isothermal vapor-liquid equilibrium measurement on (CO2 + heptane), the results of which were found to be in good agreement with literature data.In this work, we report experimental measurements of the phase behaviour and density of (CO2 + synthetic crude oil) mixtures. The 'dead' oil contained a total of 17 components including alkanes, branched-alkanes, cyclo-alkanes, and aromatics. Solution gas (0.81 methane + 0.13 ethane + 0.06 propane) was added to obtain live synthetic crudes with gas-oil ratios of either 58 or 160. Phase equilibrium and density measurements are reported for the 'dead' oil and the two 'live' oils under the addition of CO2. The measurements were carried out at temperatures of (298.15, 323.15, 373.15 and 423.15) K and at pressures up to 36 MPa, and included vapor-liquid, liquid-liquid and vapor-liquid-liquid equilibrium conditions.The results are qualitatively similar to published data for mixtures of CO2 with both real crude oils or and simple hydrocarbon mixtures containing both light and heavy components. The present experimental data have been compared with results calculated with two predictive 2 models, PPR78 and PR2SRK, based on the Peng-Robinson 78 (PR78) and Soave-RedlichKwong (SRK) equations of state with group-contribution formulae for the binary interaction parameters. Careful attention was paid to the critical constants and acentric factor of high molar-mass components. Since the mixture also contained several light substances with critical temperatures below some or all experimental temperatures, we investigated the use of the Boston-Mathias modification of the PR78 and SRK equations. The results showed that these models can predict with reasonable accuracy the vapor-liquid equilibria of systems containing CO2 and complex hydrocarbon mixtures without the need to regress multiple binary parameters against experimental data.

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Section: Evaluation Of the Critical Propertiesmentioning

confidence: 88%

Section: Ppr78 and Pr2srkmentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

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Experimental and modeling study of the phase behavior of synthetic crude oil+CO2

Ghafri

Maitland

Trusler

2014

Fluid Phase Equilibria

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“…In addition, using the previously mentioned mathematical equation relating k PR ij and k SRK ij , the PPR78 model [3][4][5][6][7][8][9][10][11][12][13][14][15][16] which may be seen as a group contribution method for the estimation of the temperature-dependent BIPs of the widely spread PR-EoS, was used to generate k ij for the SRK EoS. It is shown how the group interaction parameters initially determined for the PR-EoS [3][4][5][6][7][8][9] can be simply used to predict the temperature-dependent BIPs for the SRK EoS.…”

Section: Introductionmentioning

confidence: 99%

Relationship between the binary interaction parameters (kij) of the Peng–Robinson and those of the Soave–Redlich–Kwong equations of state: Application to the definition of the PR2SRK model

Jaubert

Privat

2010

Fluid Phase Equilibria

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152

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“…Thus, in order to investigate that effect more deeply, some (CO 2 + C 10 H 18 ) binary data found in Mehl [32], Vitu et al [33] and Silva [34] were added to the graphs. In fact, the presence of the aqueous phase causes the dew point curve to shift downward, and the dew point pressure decreases more steeply with the increase of temperature.…”

Section: Co 2 + C 10 H 18 + H 2 O Systemmentioning

confidence: 99%

Effect of water content on the equilibrium pressure of (carbon dioxide+decane and+decalin) from T=(313.15 to 333.15)K

Rocha

Fialho

Marques

et al. 2013

The Journal of Chemical Thermodynamics

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High-pressure phase behaviour of the binary system {CO2+cis-decalin} from (292.75 to 373.75)K

Cited by 17 publications

References 28 publications

Experimental and modeling study of the phase behavior of synthetic crude oil+CO2

Experimental and modeling study of the phase behavior of synthetic crude oil+CO2

Relationship between the binary interaction parameters (kij) of the Peng–Robinson and those of the Soave–Redlich–Kwong equations of state: Application to the definition of the PR2SRK model

Effect of water content on the equilibrium pressure of (carbon dioxide+decane and+decalin) from T=(313.15 to 333.15)K

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