Osmotic and activity coefficients of sodium hydroxide in water from 150 to 250.degree.C

Campbell, A. N.; Bhatnagar, Om N.

doi:10.1021/je00036a020

Cited by 35 publications

(7 citation statements)

References 7 publications

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“…(3.58-3.98) * 10 −5 Akhumov and Vasil'ev, 1932, 1936 KCl + NaCl , 1980, 1982, 1984 Non-aqueous components Campbell and Bhatnagar, 1984;Barry et al, 1988;Abdulagatov and Azizov, 2004a,b, etc.). There are the arrangements (Morey and Chen, 1956;Liu and Lindsay, 1970;Campbell and Bhatnagar, 1979;Wood et al, 1984;Emons et al, 1986;Stepanov et al, 1996, etc.…”

Section: Experimental Methods For Studying Hydrothermal Phase Equilibriamentioning

confidence: 99%

Phase Equilibria in Binary and Ternary Hydrothermal Systems

Valyashko¹

2008

Hydrothermal Experimental Data

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Section: Experimental Methods For Studying Hydrothermal Phase Equilibriamentioning

confidence: 99%

Phase Equilibria in Binary and Ternary Hydrothermal Systems

Valyashko¹

2008

Hydrothermal Experimental Data

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“…This procedure also fit the interaction parameters between the ions and water and between the cations and anions. Literature data were used to fit these parameters, as well as to fit the interaction parameter between water and acetic acid, and files containing this literature data can be found from the OSF project accompanying this article (). − Optimization was performed using the differential evolution solver implemented in the SciPy package for Python. , All the PC-SAFT parameters used or fit in this study are given in Table .…”

Section: Modelingmentioning

confidence: 99%

Vapor–Liquid Equilibrium of Ionic Liquid 7-Methyl-1,5,7-triazabicyclo[4.4.0]dec-5-enium Acetate and Its Mixtures with Water

et al. 2020

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Ionic liquids have the potential to be used for extracting valuable chemicals from raw materials. These processes often involve water, and after extraction, the water or other chemicals must be removed from the ionic liquid, so it can be reused. To help in designing such processes, we present data on the vapor–liquid equilibrium of the system containing protic ionic liquid 7-methyl-1,5,7-triazabicyclo[4.4.0]dec-5-enium acetate, water, acetic acid, and 7-methyl-1,5,7-triazabicyclo[4.4.0]dec-5-ene. Earlier studies have only focused on mixtures of water and an ionic liquid with a stoichiometric ratio of the ions. Here, we also investigated mixtures containing an excess of the acid or base component because in real systems with protic ionic liquids, the amount of acid and base in the mixture can vary. We modeled the data using both the ePC-SAFT and NRTL models, and we compared the performance of different modeling strategies. We also experimentally determined the vapor composition for a few of the samples, but none of the modeling strategies tested could accurately predict the concentration of the acid and base components in the vapor phase.

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“…In this equation, x i is the mole fraction; c i is the activity coefficient of the solution and index i represents water, sodium chloride or sodium hydroxide. The coefficients for the different components were obtained from [24][25][26]. For sodium chloride and sodium hydroxide, the activity coefficient was kept equal to 0.6, and as recommended by Szargut et al [24], the value 1.0 was adopted for water.…”

Section: Exergy Analysismentioning

confidence: 99%

Thermodynamic assessment of MVR implementation in multistage evaporation plants

Mady

Bresciani

Paiva

et al. 2018

J Braz. Soc. Mech. Sci. Eng.

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A study on process alternatives for reducing steam consumption was carried out in a multistage evaporation system of a chlorine-alkali industrial complex. A phenomenological model was developed, based on the mass and energy balances and on gas-liquid equilibrium correlations for the ternary mixture of caustic soda, sodium chloride and water. The design specifications of the plant were adopted as a reference to validate the mathematical model, which comprises 153 nonlinear equations. Different process conditions were simulated by taking into account the most important process variables and their effect on steam consumption. Differently from previously published studies, in which the conservation laws are mainly focused on the heat exchangers and their optimization, the present study considers the whole multistage evaporation unit. The model also enabled to evaluate the effect of changes in the plant configuration, either by considering a side product stream at a specified concentration, designated to another production unit in the industrial complex, or by including mechanical vapor recompression, which has proven to be a better solution to reduce steam consumption from the energy and exergy points of view. Results indicate an expressive decrease in steam consumption to around 1% of the original configuration. Moreover, from the exergy perspective, if the power generation is considered, the MVR is a better choice from the energy and exergy point of view. Keywords Exergy analysis Á Caustic soda production Á Evaporation process Á Mass and energy balances List of symbols b Specific exergy (kJ/kg) B Exergy flow rate (kW) This paper is an extended and revised version of a similar work presented in the

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Osmotic and activity coefficients of sodium hydroxide in water from 150 to 250.degree.C

Abstract: The vapor pressures of aqueous sodium hydroxide solution were measured from 150 to 250 °C In the concentration range of 0.32-3.7 m. The lowering of vapor pressure, AP, was used to calculate the osmotic and activity coefficients of NaOH by using Pttzer's equations.

Cited by 35 publications

References 7 publications

Phase Equilibria in Binary and Ternary Hydrothermal Systems

Phase Equilibria in Binary and Ternary Hydrothermal Systems

Vapor–Liquid Equilibrium of Ionic Liquid 7-Methyl-1,5,7-triazabicyclo[4.4.0]dec-5-enium Acetate and Its Mixtures with Water

Thermodynamic assessment of MVR implementation in multistage evaporation plants

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