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Recherche transversale
(titres de publication, de périodique et noms de colloque inclus)
2016-05-30 - Colloque/Présentation - poster - Anglais - 1 page(s)

Meunier Nicolas, Billemont Pierre, Thomas Diane , De Weireld Guy , "Dehydration of CO2 coming from oxyfuel cement kilns by Temperature Swing Adsorption (TSA) process using zeolites 5A, 13X and silica gel" in 12th International Conference on the Fundamentals of Adsorption, Friedrichshafen, Germany, 2016

  • Codes CREF : Traitement des effluents gazeux (DI3843), Technologie de l'environnement, contrôle de la pollution (DI3841), Thermodynamique chimique (DI132C), Génie chimique (DI2721), Chimie (DI1300)
  • Unités de recherche UMONS : Génie des Procédés chimiques et biochimiques (F505), Thermodynamique, Physique mathématique (F506)
  • Instituts UMONS : Institut de Recherche en Energétique (Energie)

Abstract(s) :

(Anglais) For two decades, the reduction of anthropogenic carbon dioxide emissions from industries (power plants, cement plants, petrochemical industry, …) has become one of the most crucial issue. In this context, preliminary theoretical studies have demonstrated the interest and feasibility of developing oxyfuel cement kilns to increase the CO2 concentration of the exhaust gases and thus facilitate its reuse or its conversion into valuable chemicals such as methanol. A purification step is primarily required and the process investigated relies on three successive main units which are respectively the desulphurization/denitrification, dehydration and cryogenic units[1]. This work focuses on the dehydration unit whose aim is to remove water from a rich-CO2 stream (83.9 mol% CO2, 15.9 mol% inerts and 0.2 mol% H2O) coming from the desulfurization/denitrification unit before entering the cryogenic unit to avoid the formation of ice at low temperatures. To perform the dehydration of this effluent, a Temperature Swing Adsorption (TSA) process[2] using zeolites 5A, 13X or silica gel has been chosen. In the first step of this work, the three adsorbents are studied from a thermodynamic point of view based on the experimental pure component isotherms at 30°C and pressures varying from 0 – 40 bar for CO2 and 0 – p/p0=0.99 for H2O. A kinetic study (the breakthrough curves measurements) is also performed to determine the kinetic parameters. A simulation model using the Linear Driving Force (LDF) model is implemented on Aspen Adsorption® software and based on our experimental data to predict the breakthrough curves of water on the different adsorbents. First results pointed out that zeolite 5A could be the most suitable adsorbent for this application regarding its higher adsorption capacity towards water and its longer breakthrough time in comparison to those from the other adsorbents. Another important issue of this study is related to the energy consumption of the TSA process that is directly linked to the nature of the selected adsorbent and the temperature required for its regeneration (ca. 300°C for zeolites in comparison to 150°C for silica gels). The length of the different steps of the TSA process are also optimized to reduce the global energy demand of this unit. Finally, economic (CAPEX and OPEX) considerations are presented with regard to the energetic integration, allowing a complete overview of this integrated CO2 dehydration process.