Carbon dioxide solubility in aqueous solutions of NaCl: Measurements and modeling with electrolyte equations of state (original) (raw)
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Journal of Chemical & Engineering Data, 1989
- Gillies, M. T. C ,-Based Chemicals from Hvdrogen and Carbon Monoxide; Noyes Data Corporation: Park RMge, NJ, 1982. (2) Taqul Khan, M. M.; Halligudi, S. 8.; Abdi, S. H. R. J . Mol. Catal. 1888, 45, 215. (3) Botteghl, C.; Ganzerla, R.: Lenarda, M.; Moretti, G. J. Mol. Catal. 1987, 40, 129. (4) Taqui Khan, M. M.; Halligudi, S. B.; Abdi, S. H. R. J. Mol. Catal., in press. ( 5 ) Chaudhary, V. R.; Parande, M. G.; Brahme, P. H. Ind. Eng. Chem. Experimental gas solublilty data for the C0,-water and C0,-1 wt % NaCi solution blnary systems are reported. Measurements were made at pressures up to 10 MPa and temperatures from 80 to 200 OC. A thet'modynamlc model of these systems Is also presented. The model employs the Peng-Robinson equation of state to represent the vapor phase and an empirical Henry's law constant correlation for the liquid phase. I t is shown that the salting-out effect of the 1 wt YO NaCl solution on CO, solubility Is small. Also described is a new experimental apparatus consisting of a variable-volume equllibrlum cell enclosed in a constant temperature controlled oven and the procedure used in conducting the experiments.
Journal of Chemical & Engineering Data
Experimental CO 2 solubility data in brine at high pressures and high temperatures are needed in different technologies such as carbon dioxide storage or geothermal process. A lot of data have been acquired in single-salt solutions, whereas data for mixed-salt solutions remain scarce. In this study, new carbon dioxide solubility data in salt solutions have been measured. Two synthetic brines have been studied at 323, 373, and 423 K from 1 to 20 MPa. The brine 1 is composed of a mixture of NaCl and CaCl 2 and the brine 2 is made from a mixture of NaCl, CaCl 2 , and KCl. Measurements have been carried out by conductimetric titration. In this study, 6 isotherms presenting 48 new solubility data have been reported. These results have been obtained in an original range of temperature, pressure, and salinity. In these conditions of temperature and pressure, we verified that an increase of the temperature or the salinity involves a decrease of the CO 2 solubility. On the other hand, an increase of the pressure implies an increase of the CO 2 solubility. Then, the obtained results were compared with the values calculated using PhreeSCALE and PSUCO2 models. The comparison between experimental and calculated values revealed a good agreement.
Chemical engineering transactions, 2015
The electrolyte thermodynamic models have been extensively studied for carbon dioxide – water system for the prediction of vapour liquid equilibrium at low pressures. However, no guidelines are available for selection of electrolytic models which are applicable at high pressure for prediction of thermodynamic properties. In this study, solubility prediction of limited Debye Huckel (DH), Pitzer Debye Huckel (PDH) and modified Three Characteristic Parameter Correlation (mTCPC) electrolyte models have been tested for a wide range of temperature (273 – 453 K) and pressure (0.1 – 7.2 MPa).The comparative study shows that introduction of electrolyte model improves the prediction accuracy when physical solubility of gas is low, either in high temperature or low pressure region. The mTCPC model gives improved prediction than nonelectrolyte model but requires additional parameters and complex calculations. New values for binary interaction parameters of UNIFAC for carbon dioxide – water syst...
Solubility of CO2 in Aqueous Solutions of NaCl at (30 to 60) °C and (10 to 20) MPa
Journal of Chemical & Engineering Data, 2003
The solubility of CO 2 in NaCl solutions with mass fractions of 0.01 to 0.03 was measured at (30 to 60)°C and (10 to 20) MPa. The CO 2 was dissolved in NaCl solution in a pressurized vessel, and a sample of the saturated solution was removed from the vessel. The solubility was then estimated by measuring the mass of the sample and the pressure of the dissolved gas. On the basis of this experimental data, an equation for predicting the CO 2 mole fraction x 1 in NaCl solution as a function of temperature t) (30 to 60)°C, pressure P) (10 to 20) MPa, and mass fraction, S, of NaCl) (0.01 to 0.03) was determined. H(P,T,S)/MPa) 36.1P/MPa + 3.87T/K-1097.1 + (196P/MPa + 26.9T/K-8810)S, where H is Henry's coefficient, H) P c /x 1 , P c is the partial pressure of carbon dioxide, T is the absolute temperature, and S is the mass fraction of NaCl in the aqueous solution.
Measurement and modeling of CO2 solubility in NaCl brine and CO2–saturated NaCl brine density
International Journal of Greenhouse Gas Control, 2011
CO 2 solubility data in the natural formation brine, synthetic formation brine, and synthetic NaCl+CaCl 2 brine were collected at the pressures from 100 to 200 bar, temperatures from 323 to 423 K. Experimental results demonstrate that the CO 2 solubility in the synthetic formation brines can be reliably represented by that in the synthetic NaCl +CaCl 2 brines. We extended our previously developed model (PSUCO2) to calculate CO 2 solubility in aqueous mixed-salt solution by using the additivity rule of the Setschenow coefficients of the individual ions (Na + , Ca 2+ , Mg 2+ , K + , Cl − , and SO 4 2− ). Comparisons with previously published models against the experimental data reveal a clear improvement of the proposed PSUCO2 model. Additionally, the path of the maximum gradient of the CO 2 solubility contours divides the P-T diagram into two distinct regions: in Region I, the CO 2 solubility in the aqueous phase decreases monotonically in response to increased temperature; in region II, the behavior of the CO 2 solubility is the opposite of that in Region I as the temperature increases.
Industrial & Engineering Chemistry Research, 2019
The model i.e the thermodynamic model is focused on Cubic-Plus-Association equation of state combined with Wong-Sandler mixing rule with six parameters is presented (CPA-WS). The model confirmed that the inert association scheme is more suitable for carbon dioxide (CO 2) than 3B association scheme, for the level equilibrium in Carbon dioxide-water (H 2 O) system. Meanwhile, CO 2-H 2 O-sodium chloride (NaCl) system can be reasonably well predicted by using two adjustable parameters of H 2 O-NaCl and CO 2-NaCl systems. The average absolute relative deviations in predicted CO 2 solubility in H 2 O, and aqueous NaCl solutions of CPA-WS model are 5.31% and 3.56%, respectively.
Fluid Phase Equilibria, 2012
New experimental results are presented for the solubility and the partial molar volume of carbon dioxide in an aqueous solution of phenol and sodium chloride at temperatures of about (314, 354 and 395) K and pressures up to about 10 MPa. The composition of the solventexpressed as molality in wateris about 0.5 mol/(kg H 2 O) for phenol and 1 mol/(kg H 2 O) for sodium chloride. The experimental work is a continuation of investigations on the influence of organic components and strong electrolytes on the solubility of carbon dioxide in water. It extends a data base for developing and testing thermodynamic models to describe the solubility of gases in salt-free and salt-containing aqueous solvents mixed with organic compounds. The experimental results are compared to predictions and correlations from a thermodynamic model which combines a model for the solubility of CO 2 in aqueous solutions of NaCl with a model for the solubility of CO 2 in aqueous solutions of phenol. The prediction results reveal a reasonable agreement. As in a previous investigationwith N,N-dimethylformamide instead of phenol as the organic solvent componentadjusting a ternary parameter for interactions between the three solutes (i.e. CO 2 , NaCl, and phenol) results in a correlation that allows to describe the new experimental data within experimental uncertainty. 2014 Published by Elsevier B.V.
Thermodynamic model of aqueous CO2–H2O–NaCl solutions from −22 to 100°C and from 0.1 to 100MPa
Fluid Phase Equilibria, 2010
Experimental measurements of the solubility of CO 2 in aqueous NaCl solutions have been assembled from 21 literature studies and tested for consistency using analytical and thermodynamic criteria. Of the 508 data compiled, 170 data (33%) were discarded and 36 were reserved to test the high-pressure dependency of the model. Possible reasons for the observed discrepancies between datasets are discussed. The 302 measurements that satisfy the acceptance criteria have been used to fit Pitzer parameters. These have been incorporated into a semi-empirical, -type thermodynamic model that builds upon published equations of state for the unary and binary subsystems. The accepted experimental solubilities are reproduced by the model with a precision of better than 1.6% (one standard deviation) over the entire P-T-x range considered. The new model provides a thermodynamically consistent description of numerous properties of the aqueous liquid in the ternary CO 2 -H 2 O-NaCl system, including: the activity coefficients, activities and partial molar volumes of CO 2(aq) and Na + Cl − (aq) ; the activity coefficient and osmotic coefficient of the solvent H 2 O; the Setchenow coefficient; saturation indices of all four solid phases in the system (CO 2 -clathrate-hydrate, ice, hydrohalite and halite); and the molar volume, excess molar volume and density of the bulk liquid. These properties can be calculated for any CO 2 concentration up to saturation, and for any NaCl concentration (whether stable or metastable). The model is available as a computer code at <www.geo.unibe.ch/diamond>. (N.N. Akinfiev), diamond@geo.unibe.ch (L.W. Diamond). 1 Tel.: +7 499 230 8231; fax: +7 495 951 1587. 0378-3812/$ -see front matter