Solubility of n-octadecane in supercritical carbon dioxide at 310, 313, 333, and 353 K, in the range 10–20 MPa

Eustaquio‐Rincón, Rafael; Trejo, Arturo

doi:10.1016/s0378-3812(01)00473-3

Cited by 51 publications

(16 citation statements)

References 12 publications

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“…The supercritical fluid extraction (SFE) apparatus used in this work was custom-built in our laboratory, and was a modification of a device previously used to study the solubility of saturated lineal hydrocarbons in supercritical carbon dioxide (15). A schematic representation of the experimental apparatus developed in this work is presented in Fig.…”

Section: Experimental Apparatus and Proceduresmentioning

confidence: 99%

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Extraction of Hydrocarbons from Crude Oil Tank Bottom Sludges using Supercritical Ethane

Ávila-Chávez

Eustaquio‐Rincón

Reza

et al. 2007

Separation Science and Technology

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A custom-built, solvent recirculating, supercritical fluid extraction (SFE) apparatus was used to study the extraction of hydrocarbons from a crude oil tank bottom sludge (COTBS) with supercritical ethane. The SFE experiments were carried out varying the pressure (10 MPa and 17.20 MPa) and temperature (358C and 658C). The yield of the extracted hydrocarbon fraction increased with increase in extraction pressure at constant temperature, and decreased with increase in extraction temperature at constant pressure. The maximum extraction yield was obtained at the pressure and temperature conditions that lead to the highest solvent density. The extracted hydrocarbon fraction was a significantly upgraded liquid relative to the original untreated COTBS.

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Section: Experimental Apparatus and Proceduresmentioning

confidence: 99%

“…The separation and the solvent recycling section was constituted by a recovery stainless steel cell [15]. This cell (internal volume of 60 cm 3 ) was used to reduce the pressure and temperature of the fluid leaving the extraction section in order to separate the extracted phase from the solvent.…”

Section: Experimental Apparatus and Proceduresmentioning

confidence: 99%

Extraction of Hydrocarbons from Crude Oil Tank Bottom Sludges using Supercritical Ethane

Ávila-Chávez

Eustaquio‐Rincón

Reza

et al. 2007

Separation Science and Technology

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“…High-pressure phase equilibria of systems containing hydrocarbons and CO2 are also of interest in a wide range of industrial processes such as hydro-treatment of aqueous waste streams [13], production of coal liquids and petroleum processing [14], separation processes [15], and supercritical fluid extraction [16,17]. In addition, supercritical CO2 is used as a solvent on both laboratory and industrial scales [18] for reactions such as hydrogenation [19] hydroformylation [20] and polymerization [21,22].…”

Section: Introductionmentioning

confidence: 99%

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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“…In 2001, Eustaquio-Rincon and Trejo [35] measured the solubility of n-octadecane in supercritical carbon dioxide at four different temperatures (310, 313, 333, and 353) K for the pressure range (10 to 20) MPa. In 2002, Nieuwoudt and du Rand [36] measured high pressure phase equilibria of supercritical carbon dioxide with n-alkanes (n-dodecane, n-hexadecane, neicosane, n-tetracosane, n-octacosane, and n-hexatriacontane) over the temperature range (313 to 367) K. Tsuji et al [37] measured the bubble point pressure and liquid density data for (carbon dioxide + decane) system at 344.3 K. In 2006, Jiménez-Gallegos et al [38] measured the (vapor + liquid) equilibria for systems (carbon dioxide + octane) and (carbon dioxide + decane) from (322 to 372) K and (319 to 372) K, respectively.…”

Section: Introductionmentioning

confidence: 99%

Phase composition and saturated liquid properties in binary and ternary systems containing carbon dioxide, n-decane, and n-tetradecane

Kariznovi

Nourozieh

Abedi

2013

The Journal of Chemical Thermodynamics

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Solubility of n-octadecane in supercritical carbon dioxide at 310, 313, 333, and 353 K, in the range 10–20 MPa

Cited by 51 publications

References 12 publications

Extraction of Hydrocarbons from Crude Oil Tank Bottom Sludges using Supercritical Ethane

Extraction of Hydrocarbons from Crude Oil Tank Bottom Sludges using Supercritical Ethane

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

Phase composition and saturated liquid properties in binary and ternary systems containing carbon dioxide, n-decane, and n-tetradecane

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