Calculation of phase equilibrium in supercritical extraction of C54 triglyceride (rapeseed oil)

Geană, Dan; Steiner, Rudolf

doi:10.1016/0896-8446(95)90023-3

Cited by 22 publications

(22 citation statements)

References 15 publications

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“…One of the hard sphere equations of state, equations. (6)- (11), can replace the unperturbed term in the equations (2) or (3).…”

Section: Hard Sphere Equation Of Statementioning

confidence: 98%

“…This theory has the advantage of having a sound thermodynamic basis the compressibility factor, Z, can be written as: In the perturbation theory, the total compressibility factor is divided into a reference part and a perturbed part such as; (2) where Z 0 is the reference system and called Z unperturbed . The perturbed part, Z perturbed , is expressed in the form of a series, ∑ a i Z i , which takes into account all other possible factor may involved in the compressibility factor.…”

Section: Derivation Of the Equation Of Statementioning

confidence: 99%

“…In addition, properties of compounds such as vapor pressure, density of vapor and liquid, thermal properties, and solubility of substances in supercritical fluids are calculated by using equations of state [1][2][3][4][5]. From the many equations of state, cubic equations of state are currently the equations of state considered most applicable for such calculations.…”

Section: Introductionmentioning

confidence: 99%

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A Two Parameters Equation of State for Phase Equilibrium Behaviour Reservoir and Liquified Natural Gas

Hosseinbeigi

Pazuki²,

Edalat

2005

Canadian International Petroleum Conference

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Based on molecular theory of hard-core model. The parameters of the ne In this study, an equation of state is derived w cubic equation of state are temperature and acentric factor dependent. To calculate the saturate vapor pressure and volume of vapor and liquid of pure compound, this equation of state requires the critical temperature, the critical pressure and acentric factor of the compound. The proposed equation of state is applied for the calculation of PVT and VLE of various pure fluids and fluid mixtures. The average of absolute deviations of the predicted vapor pressure, vapor volume and saturated liquid density of 30 pure compounds are 0.814, 2.614 and 5.814%, respectively. The results are compared with those obtained by commonly used cubic equations of state. In addition comparisons with the mentioned cubic equations of state to predict some of the thermodynamic properties, including second virial coefficients and thermal properties, are given. The results indicate that the new equation of state yields better results. Moreover, the capability of the equation of state to predict the molar heat capacity of gases at constant pressure and volume, the sound velocity in gases, and the zero line fpr gases are also illustrated.

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“…One of the hard sphere equations of state, equations. (6)- (11), can replace the unperturbed term in the equations (2) or (3).…”

Section: Hard Sphere Equation Of Statementioning

confidence: 98%

Section: Derivation Of the Equation Of Statementioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

See 1 more Smart Citation

A Two Parameters Equation of State for Phase Equilibrium Behaviour Reservoir and Liquified Natural Gas

Hosseinbeigi

Pazuki²,

Edalat

2005

Canadian International Petroleum Conference

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“…Reliable high-pressure vapor-liquid equilibrium (VLE) data over a wide range of pressures and temperatures, and development of simple thermodynamic models provide basic, necessary information for the process development and economic evaluation of the extraction and the fractionation processes. Although many single component VLE data and modeling works are presented in open literature [15][16][17][18][19][20][21][22], only few works concerning multicomponent VLE data and thermodynamic modeling have been published [23][24][25][26]. In addition, some of these works are suffered from limited phase equilibria data at narrow temperature or pressure range, and complexity and low applicability of thermodynamic models.…”

Section: Introductionmentioning

confidence: 99%

Phase equilibria of palm oil, palm kernel oil, and oleic acid+supercritical carbon dioxide and modeling using Peng–Robinson EOS

Hong

Kim

et al. 2010

Journal of Industrial and Engineering Chemistry

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“…By correlating limited experimental data gained from literature using thermodynamic models, a general representation of the phase behavior of a system can be determined, thus making it possible to reduce experimental work. The equation of state has been shown to adequately represent the phase behavior of lipid-related components with supercritical CO 2 (2)(3)(4)(5). It is anticipated that the equation of state also can model the phase equilibrium of a palm oil components-supercritical CO 2 system.…”

mentioning

confidence: 99%

Simulation modeling of the phase behavior of palm oil‐supercritical carbon dioxide

Lim

Manan

Sarmidi

2003

J Americ Oil Chem Soc

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The phase behavior of crude palm oil (CPO) with supercritical CO 2 was successfully modeled in an Aspen Plus ® 10.2.1 commercial simulator (Aspen Technology Inc., Cambridge, MA) using the Redlich-Kwong-Aspen (RKA) equation of state thermodynamic model. The modeling procedure involved estimating pure component vapor pressures and critical properties and computing a regression of phase equilibrium behavior. The interaction parameters for the RKA model were obtained from the regression of experimental phase equilibrium data for a binary system of palm oil components-supercritical CO 2 available in the literature. The distribution coefficients and solubilities of palm oil components obtained from this simulation showed good agreement with experimental data obtained from the literature. The model provides an efficient and cost-effective alternative for the preliminary design and optimization of a supercritical fluid extraction process involving a complex CPO-supercritical CO 2 system.Over the years, supercritical fluid extraction (SFE) technology has developed rapidly and found applications in the commercial production of vegetable oils, including palm oil. Palm oil contains various components such as MG (<1%), DG (2-7%), TG (>90%), FFA (3-5%), phospholipids, pigmented compounds, and several nutritionally bioactive compounds (1). Minor components such as β-carotene and tocopherol are often degraded or lost during the bleaching and refining processes, which require high operating temperatures of up to 240°C. Selective supercritical CO 2 extraction of these highvalue but thermally unstable components from crude palm oil (CPO) has enabled operation at mild temperatures of less than 100°C. In addition, the inert solvent used can be easily separated and recovered, thereby leading to a pollution-free operation. All these advantages combine to make SFE of components in palm oil a desirable alternative to conventional processing methods such as chemical and physical refining.By correlating limited experimental data gained from literature using thermodynamic models, a general representation of the phase behavior of a system can be determined, thus making it possible to reduce experimental work. The equation of state has been shown to adequately represent the phase behavior of lipid-related components with supercritical CO 2 (2-5). It is anticipated that the equation of state also can model the phase equilibrium of a palm oil components-supercritical CO 2 system. However, a reliable phase equilibrium model is required in the analysis of the SFE process involving a palm oil-supercritical CO 2 system since the system comprises a highly dissimilar mixture of high M.W. TG and low M.W. supercritical CO 2 . In addition, such a model must be applicable over a wide range of temperatures and pressures to yield some accurate quantitative values of the mutual solubilities, compositions of coexisting phases, and distribution coefficients that are of fundamental importance in the design of a countercurrent SFE process. The steps involved in...

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Calculation of phase equilibrium in supercritical extraction of C54 triglyceride (rapeseed oil)

Cited by 22 publications

References 15 publications

A Two Parameters Equation of State for Phase Equilibrium Behaviour Reservoir and Liquified Natural Gas

A Two Parameters Equation of State for Phase Equilibrium Behaviour Reservoir and Liquified Natural Gas

Phase equilibria of palm oil, palm kernel oil, and oleic acid+supercritical carbon dioxide and modeling using Peng–Robinson EOS

Simulation modeling of the phase behavior of palm oil‐supercritical carbon dioxide

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