Phase diagrams for ternary salt solutions
Phase diagrams for ternary salt solutions
Phase diagrams for ternary salt solutions are very useful for designing processes with salt solutions such as fractional crystallization processes. The phase diagrams shown on this page were calculated with the Extended UNIQUAC model.
Several phase diagrams for ternary salt solutions are shown in the tabs below. This includes:
- Partial pressures in the carbon dioxide – ammonia – water system
Solubility diagrams for the following systems are shown:
- Sodium nitrate – sodium sulfate – water
- Sodium sulfate – magnesium sulfate – water
- Magnesium sulfate – potassium sulfate water
- Sodium chloride – sodium nitrate – water
- Sodium hydroxide – phosphoric acid – water.
The carbon dioxide – ammonia – water system
The phase behavior and the thermal properties of this system is important because of its potential use for removing carbon dioxide from flue gas in post combustion carbon capture processes.
One such process is the chilled ammonia process (Eli Gal, Ultra cleaning combustion gas including the removal of CO2, United States Patent US7641717B2.
In the chilled ammonia process, a slurry consisting of a liquid in equilibrium with solid ammonium bicarbonate (NH4HCO3) is produced in an absorber. The slurry releases CO2 at a relatively high pressure after being heated in a desorber. The liquid is cooled and led back to the absorber for a new cycle.
The CO2 – NH3 – H2O system was modeled with the Extended UNIQUAC model. (Thomsen K and Rasmussen P, “Modeling of Vapor-liquid-solid equilibrium in gas-aqueous electrolyte systems”, Chemical Engineering Science, 54(1999)1787-1802. An upgraded version of this model valid to higher temperatures and more accurate was published by Victor Darde, Willy J.M. van Well, Erling H. Stenby, Kaj Thomsen, “Modeling of carbon dioxide absorption by aqueous ammonia solutions using the Extended UNIQUAC model”, Ind. Eng. Chem. Res., 49(2010), pp 12663–12674 (24), https://doi.org/10.1021/ie1009519.
The figures show the experimentally measured and the calculated speciation in a 6.226 molal NH3 solution at 40°C. The amount of carbamate formed is indicated in the figure to the left with red triangles (experimental) and a red line (calculated with the Extended UNIQUAC model).
The amounts of NH3, NH4+, and NH2COO– are shown in the figure to the left, the amounts of CO2, CO32-, and HCO3– in the same solution are shown to the right. The experimental data were measured by Ute Lichtfers and published in her PhD Dissertation, University of Kaiserslautern, Germany, 2000. The lines were calculated with the Extended UNIQUAC model. There is a good agreement between the experimental data and the corresponding calculated values. It is seen that the amount of carbamate apparently goes through a maximum at approximately 3 mol CO2 per kg water. This maximum occurs at a pH about 9 and at a loading of 0.5 mol CO2 per mol NH3.
The figures below show vapor-liquid equilibrium in the CO2-NH3-H2O system at 20°C. Calculated and experimental partial pressure of ammonia shown to the left. Calculated and experimental partial pressure of carbon dioxide shown to the right. The experimental data are from
- Van Krevelen D.W., Hoftijzer P.J., Huntjens F.J., Recueil des travaux chimiques des Pays-Bas, 68(1949)191-216, https://doi.org/10.1002/recl.19490680213;
- Pexton S., Badger E.H.M., Journal of the Society of Chemical Industry, 57(1938)107-110; The Society of Chemical Industry
- Otsuka E., Yoshimura S., Yakabe M., Inoue S., Kogyo Kagaku Zasshi, 62(1960)1214-8. The Chemical Society of Japan
Precise vapor-liquid equilibrium calculations are important for designing processes such as carbon capture processes using ammonia. The Extended UNIQUAC model was fitted to experimental data in the temperature range from 0 to 110°C and is able to reproduce data with high accuracy in this temperature range and at pressures up to 100 bar. At temperatures above 110°C the accuracy is decreasing.
Sample calculations performed with the Extended UNIQUAC model are shown below. The calculated data are compared with experimental values in order to document the quality of the fit. Partial pressures of NH3 are shown in the figures to the left, partial pressures of CO2 are shown in the figures to the right. The calculations were performed for solutions containing a fixed amount of ammonia while different amounts of carbon dioxide were added. Each ammonia concentration is represented by a branch in the diagram.
It is seen that the partial pressure of ammonia is decreasing by the addition of CO2 while the CO2 partial pressure is increasing. At a loading of approximately 1 mol of CO2 per mole NH3, the partial pressure of CO2 is seen to increase rapidly. This is because ammonia and carbon dioxide react one to one. When the available ammonia is neutralized by carbon dioxide, the vapor pressure of carbon dioxide goes up because the solubility of CO2 in solutions with low pH is not very high.
The figures above show vapor-liquid equilibrium in the CO2-NH3-H2O system at 80°C. Calculated and experimental partial pressure of ammonia shown to the left. Calculated and experimental partial pressure of carbon dioxide shown to the right. The experimental data are from:
In the original concept of the chilled ammonia process, solid NH4HCO3 is formed in the absorber. It is therefore important to be able to calculate solid-liquid equilibrium in the system accurately.
The available experimental data for solid-liquid equilibrium in the system are scarce and they are inconsistent. The researchers who reported on solid liquid equilibrium in the system do not agree on what solid phases are formed in the system.
It was found that the experimental data reported by Jänecke, seemed to be most reliable and were given highest weight when determining parameters in the model.
The experimental data plotted in the solid-liquid phase diagram are from:
- Jänecke E, Zeitschrift für Elektrochemie, 35(1929)716-728; https://doi.org/10.1002/bbpc.192900060
- Terres E and Weiser H, Zeitschrift für Elektrochemie, 27(1921)177-193; https://doi.org/10.1002/bbpc.19210270901
- Terres E and Behrens H, Zeitschrift für physikalische Chemie, 139(1928)695-716. https://doi.org/10.1515/zpch-1928-13943
These solids will precipitate from a chilled ammonia solution of sufficient ammonia concentration when carbon dioxide is added (the solution is loaded with carbon dioxide).
Due to constraints caused by Gibbs Phase rule, the two partial pressures remain constant while two solid phases are present simultaneously. In a three component system with four phases, there is only one degree of freedom (see invariant points). If the composition of the gas phase or of the liquid phase is changed, the pressure will change. If the total pressure and the temperature are kept constant, the composition of the gas or of the liquid therefore can not change.
The overall reaction taking place as CO2 is added to the system is: CO2(g) + (NH4)2CO3·H2O(s) ↔ 2NH4HCO3(s).
This is shown in the figure below for a temperature of 10°C, a total pressure of 1 bar and a 27 wt% ammonia in water solution. In the rightmost figure below, the partial pressures of carbon dioxide and ammonia as function of CO2 loading are shown. At low loadings, ammonium carbonate monohydrate is precipitating. The partial pressure of ammonium is decreasing as carbon dioxide is added, and that of carbon dioxide is slightly increasing. As the loading increases, pH of the solution decreases and at a loading slightly above 0.5, ammonium bicarbonate becomes superaturated and starts precipitating. The number of solid phases is therefore two and the total number of phases is four. The system has only one degree of freedom. When carbon dioxide is added, the amount of solid ammonium carbonate is increasing and the amount of solid ammonium carbonate monohydrate is decreasing. At a loading of 0.78, the last ammonium carbonate monohydrate has disappeared. The system now has only one solid phase, one liquid phase and a gas phase. Two degrees of freedom are available and the vapor pressure increases upon further loading with carbon dioxide.
The graph to the left below shows the amounts of solids precipitating from a solution consisting of approximately one kilo water. The precipitated amount of ammonium carbonate monohydrate reaches a maximum at a loading of 0.51. At a loading of 0.78 mol CO2/mol NH3, the last ammonium carbonate monohydrate has disappeared.
The kinetics of this solid-solid transition has not been described in the literature and it is not known if the CO2 absorption or the solid-solid transition is the rate limiting step for the absorption process.
The rightmost figure below shows the partial pressures of carbon dioxide and ammonia during loading of a 27 wt% ammonia solution with carbon dioxide. The figure to the left shows the corresponding amounts of the two solids present in this loading range. These amounts are based on a solution with approximately 1 kg water. The graphs were calculated for 10°C and for a 27 wt% ammonia in water solution. The same scenario is valid in a wide temperature range. When the loaded slurry is heated to 50°C all ammonium bicarbonate seems to dissolve in the solution.
The graphs were calculated using the Extended UNIQUAC model implemented in a DLL fille that is called from Microsoft Excel®. Vapor-liquid-solid equlibrium flash calculations are performed by calling the DLL file through the Visual Basic interface.