Abstract
The statistical associating fluid theory equation of state (EoS) is employed in a time efficient way for the correlation and prediction of vapor–liquid equilibrium of the CO2 + H2O binary system for the temperature (10–100 °C) and pressure (1–600 bar) ranges suitable for simulation of CO2 geologic sequestration. The effective number of segments and energy parameter are correlated with the reduced temperature. Simple mixing rules are applied to obtain binary interaction parameters. Assigning a fixed H2O composition in the mixing rule makes the phase equilibrium calculations relatively fast compared to other EoS’s. The results obtained by the model used were found to be in satisfactory agreement with the literature data.
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Abbreviations
- A :
-
Helmholtz energy (J)
- d :
-
Hard-sphere diameter (10−10 m)
- g :
-
Radius distribution function
- k :
-
Boltzman-constant (J·K−1)
- M :
-
Number of associated sites
- N :
-
Number of molecules
- N AV :
-
Avogadro’s number (6.02217 × 1023 mol−1)
- p :
-
Pressure (bar)
- P c :
-
Critical pressure (for CO2 73.83 bar, for H2O 220.55 bar)
- T c :
-
Critical temperature (for CO2 304.2 K, for H2O 647.1 K)
- T :
-
Absolute temperature (K)
- t :
-
Celsius temperature (°C) (T/K) −273.15
- R :
-
Gas constant (J·K−1·mol−1)
- x :
-
Mole fraction in liquid phase
- \( X_{i}^{A} \) :
-
Mole fraction of molecule i not bonded at site A
- y :
-
Mole fraction in vapor phase
- Z :
-
Compressibility factor
- β :
-
1/KT
- \( \frac{\varepsilon }{k} \) :
-
Energy parameter of dispersion (K)
- \( \frac{{\varepsilon^{AB} }}{k} \) :
-
Energy parameter of association between sites A and B
- \( \kappa^{AB} \) :
-
Bonding volume
- \( \Delta^{AB} \) :
-
Association strength between sites A and B
- μ :
-
Chemical potential
- \( \rho \) :
-
Molar density (mol·m−3)
- \( \rho_{n} \) :
-
Number density (m−3)
- A, B, C, D, E, F :
-
Constants
- abs:
-
Absolute
- assoc:
-
Association interaction
- chain:
-
Hard-sphere chain
- disp:
-
Dispersion interaction
- hs:
-
Hard sphere
- obj:
-
Objective function
- lit:
-
Literature value
- cal:
-
Calculated value
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Acknowledgments
The work was conducted with the support of the Reservoir Simulation Joint Industry Project, a consortium of operating and service companies for Petroleum and Geosystems Engineering at The University of Texas at Austin.
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Appendices
Appendix
This section provides necessary functions to calculate chemical potential μ i , compressibility factor Z, and fugacity coefficient \( \varphi_{i} \). First, μ i , which is a derivative of \( A^{\rm {res}} \) with respect to the mole number of component i at constant T, volume \( V \), and non-i components, is shown.
Expression for Chemical Potential
We discuss \( \mu_{i} \) in the order used to present the corresponding Helmohltz energy terms, i.e., hard-sphere, chain, dispersion, and association terms. The expression is:
The hard-sphere contribution to the chemical potential, \( \mu_{i}^{\rm {hs}} \), can be expressed as:
\( \mu_{i}^{\rm {chain}} \), the chain contribution to the chemical potential, is expressed as:
where
The dispersion contribution to the chemical potential, \( \mu_{i}^{\rm {disp}} \) is expressed as:
where
\( \mu_{i}^{\rm {assoc}} \), the association contribution to the chemical potential can be expressed as:
where
\( \left( {\frac{{\partial X^{{B_{k} }} }}{{\partial \rho_{i} }}} \right)_{{T,\rho_{l \ne i} }} \) and so forth can be found similarly following Eq. 34. Now the expression for \( \left( {\frac{{\partial \Delta^{{A_{j} B_{k} }} }}{{\partial \rho_{i} }}} \right)_{{T,\rho_{l \ne i} }} \)is given by:
where
Expression for Compressibility Factor Z
The compressibility factor is calculated from the Helmholtz energy, A, through:
where:
and
Here \( \mu_{i}^{\rm {assoc}} \)and \( A^{\rm {assoc}} \)are presented by Eqs. 33 and 20, respectively.
Expression for Fugacity Coefficient
The relation between \( \varphi_{i} \)(fugacity coefficient) and the residual chemical potential of component i is as follows:
\( \mu_{i}^{\rm {res}} \) and Z can be obtained from Eqs. 25 and 37, respectively.
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Islam, A.W., Sepehrnoori, K. & Patzek, T.W. A Computationally Efficient Approach to Applying the SAFT Equation for CO2 + H2O Phase Equilibrium Calculations. J Solution Chem 43, 241–254 (2014). https://doi.org/10.1007/s10953-013-0119-2
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DOI: https://doi.org/10.1007/s10953-013-0119-2