Modeling of Carbon Dioxide Absorption by Aqueous Ammonia Solutions Using the Extended UNIQUAC Model

2010 ◽  
Vol 49 (24) ◽  
pp. 12663-12674 ◽  
Author(s):  
Victor Darde ◽  
Willy J. M. van Well ◽  
Erling H. Stenby ◽  
Kaj Thomsen
Keyword(s):  
Carbon Dioxide ◽  
Aqueous Ammonia ◽  
Carbon Dioxide Absorption ◽  
Uniquac Model ◽  
Extended Uniquac ◽  
Extended Uniquac Model

Process simulation of CO2 capture with aqueous ammonia using the Extended UNIQUAC model

2012 ◽  
Vol 10 ◽  
pp. 74-87 ◽  
Author(s):  
Victor Darde ◽  
Bjørn Maribo-Mogensen ◽  
Willy J.M. van Well ◽  
Erling H. Stenby ◽  
Kaj Thomsen
Keyword(s):  
Co2 Capture ◽  
Process Simulation ◽  
Aqueous Ammonia ◽  
Uniquac Model ◽  
Extended Uniquac ◽  
Extended Uniquac Model

Modeling the solubility of carbon dioxide in the MDEA + AEEA aqueous solution using the SAFT-HR equation of state and extended UNIQUAC model

2021 ◽  
pp. 1-17
Author(s):  
Azam Najafloo ◽  
Hossein Sakhaeinia
Keyword(s):  
Carbon Dioxide ◽  
Aqueous Solution ◽  
Liquid Phase ◽  
Equation Of State ◽  
Chemical Equilibrium ◽  
Extended Uniquac ◽  
Extended Uniquac Model ◽  
Point Calculation ◽  
Interior Loop ◽  
Fugacity Coefficients

In this study, a thermodynamic model has been used to determine the solubility of carbon dioxide in an aqueous solution which is the combination of methyldiethanolamine (MDEA) and aminoethylethanolamine (AEEA). The physical equilibriums have been considered between the liquid and vapor phases and chemical equilibrium in the liquid phase. The SAFT-HR equation of state has been used to specify the fugacity coefficients of the components in the vapor phase. The liquid phase is considered as an electrolyte solution besides; the extended UNIQUAC has been applied to figure out the activity coefficients. The bubble point calculation has been used in this research. This method includes two main loops. Calculations related to chemical equilibrium are performed in the interior loop and the ones associated with phase equilibrium are done in the exterior loop. The solubility of carbon dioxide has been predicted by the optimized parameters of the model in the temperature range of 308.2–368.2 K. It has been calculated that the absolute average relative deviations of the model are 16.65, 19.33, 28.91 and 19.99 in the calculation of partial pressure of carbon dioxide in various loadings at the temperatures of 308.2, 328.2, 343.2 and 368.2 K.

Liquid-Liquid Equilibria for Linalool in Aqueous Alcohol Mixtures

2013 ◽  
Vol 634-638 ◽  
pp. 1022-1025 ◽  
Author(s):  
Heng De Li ◽  
Cheng Huang ◽  
Xiao Zhong Ma ◽  
Yu Qing Feng
Keyword(s):  
Atmospheric Pressure ◽  
Ternary Mixtures ◽  
Aqueous Alcohol ◽  
Liquid Equilibrium ◽  
Uniquac Model ◽  
Extended Uniquac ◽  
Extended Uniquac Model ◽  
Equilibrium Data ◽  
Ethanol System ◽  
Tie Line

Liquid-liquid equilibrium tie-line data were examined at atmospheric pressure and at 298.15 K for ternary mixtures of (water + methanol + linalool) as well as (water + ethanol + linalool). The distribution ratios of alcohol between organic and aqueous phases are discussed. The immiscible area of (water + methanol + linalool) system is wider than that for the ethanol system. The experimental liquid–liquid equilibrium data were satisfactorily fitted by means of an extended UNIQUAC model.

Activity Coefficient Modelling of Aqueous Solutions of Alkyl Ammonium Salts using the Extended UNIQUAC Model

2016 ◽  
Vol 45 (10) ◽  
pp. 1434-1452 ◽  
Author(s):  
Vahid Akbari ◽  
Mohammad Reza Dehghani ◽  
Tohid Nejad Ghaffar Borhani ◽  
Abbas Azarpour
Keyword(s):  
Activity Coefficient ◽  
Aqueous Solutions ◽  
Ammonium Salts ◽  
Uniquac Model ◽  
Extended Uniquac ◽  
Extended Uniquac Model ◽  
Alkyl Ammonium
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