Mathematical Model for the Gasification of Coal under Pressure

Macák, Jan; Malecha, J.

doi:10.1021/i260065a017

Cited by 137 publications

(9 citation statements)

References 3 publications

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“…Several modelling and simulation studies have been carried out for biomass and coal gasification based on a selection of the literature kinetics data [10,22,[29][30][31][32][33][34][35][36][37][38][39]. The kinetics parameters for the reactions in Table 1 are referred from the literature listed in Table 2.…”

Section: Reaction Kineticsmentioning

confidence: 99%

Biomass Steam Gasification with In-Situ CO2 Capture for Enriched Hydrogen Gas Production: A Reaction Kinetics Modelling Approach

et al. 2010

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Due to energy and environmental issues, hydrogen has become a more attractive clean fuel. Furthermore, there is high interest in producing hydrogen from biomass with a view to sustainability. The thermochemical process for hydrogen production, i.e. gasification, is the focus of this work. This paper discusses the mathematical modeling of hydrogen production process via biomass steam gasification with calcium oxide as sorbent in a gasifier. A modelling framework consisting of kinetics models for char gasification, methanation, Boudouard, methane reforming, water gas shift and carbonation reactions to represent the gasification and CO 2 adsorption in the gasifier, is developed and implemented in MATLAB. The scope of the work includes an investigation of the influence of the temperature, steam/biomass ratio and sorbent/biomass ratio on the amount of hydrogen produced, product gas compositions and carbon conversion. The importance of different reactions involved in the process is also discussed. It is observed that hydrogen production and carbon conversion increase with increasing temperature and steam/biomass ratio. The model predicts a maximum hydrogen mole fraction in the product gas of 0.81 occurring at 950 K, steam/biomass ratio of 3.0 and sorbent/biomass ratio of 1.0. In addition, at sorbent/biomass ratio of 1.52, purity of H 2 can be increased to 0.98 mole fraction with all CO 2 present in the system adsorbed.

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Section: Reaction Kineticsmentioning

confidence: 99%

Biomass Steam Gasification with In-Situ CO2 Capture for Enriched Hydrogen Gas Production: A Reaction Kinetics Modelling Approach

et al. 2010

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“…Gómez -Biba (Biba et al, 1978;Franks, 1967;Gómez-Barea and Leckner, 2010;Yoon et al, 1978) Snider -Bustamante (GRI) -Moe (Bradford, 1933;Bustamante et al, 2004;Bustamante et al, 2005;Smith et al;Snider et al, 2011) Wang -Lindstedt -Kuo (Jones and Lindstedt, 1988;Kuo, 1986;Wang et al, 2012) = 2,38 • 10 3 Corella and more (Corella and Sanz, 2005;González-Saiz, 1988;Simell et al, 1999;Xu and Froment, 1989) = 2,50 • 10 5 Maki (Maki and Miura, 1997;Modell and Reid, 1974) For the water-gas shift reaction, the several sources for the reaction rate expression shows a wide variety of reaction rates. Eikeland et al (Eikeland et al, 2015) refer to Umeki et al (Umeki et al, 2010).…”

Section: Referring Sourcementioning

confidence: 99%

“…refers to Corella and Sans (Corella and Sanz, 2005), but are using the GRI expressions referred by Snider et al (Snider et al, 2011) from Bustamante (Bustamante et al, 2004;Bustamante et al, 2005). Xie et al (Xie et al, 2012) refers to Gómez-Barea and Leckner (Gómez-Barea and Leckner, 2010), who refers to Biba et al (Biba et al, 1978) referring to a book by Franks (Franks, 1967). Biba et al (Biba et al, 1978) points out that values determined by experiments for the frequency factor cited in the literature are strictly dependent on the form of the carbonaceous material being examined, on the specific surface area, and on the corresponding value of activation energy.…”

Section: Referring Sourcementioning

confidence: 99%

“…Xie et al (Xie et al, 2012) refers to Gómez-Barea and Leckner (Gómez-Barea and Leckner, 2010), who refers to Biba et al (Biba et al, 1978) referring to a book by Franks (Franks, 1967). Biba et al (Biba et al, 1978) points out that values determined by experiments for the frequency factor cited in the literature are strictly dependent on the form of the carbonaceous material being examined, on the specific surface area, and on the corresponding value of activation energy. They have chosen mean values of literature data, and then made a sensitivity analysis for their mathematical model.…”

Section: Referring Sourcementioning

confidence: 99%

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Screening of Kinetic Rate Equations for Gasification Simulation Models

Solli

Thapa

Moldestad

2018

Linköping Electronic Conference Proceedings

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The energy from biomass can be utilized through the thermochemical conversion process of pyrolysis and gasification. The process involves solid phase and fluid phase interactions. Computational Particle Fluid Dynamics (CPFD) tools are most commonly used for simulations. The chemical processes involved is described by reaction rate expressions and equilibrium constants. These expressions are often not well studied, but rather adapted from previous studies in lack of better knowledge. Methodology and tools are presented to aim in the selection and optimization of rate expressions for a particular process. Simulation tools for reactions in batch or plug-flow conditions are shown applicable to study selected chemical reactions in detail. Results from one such study is compared to CPFD as well as CSTR results of a gasification process. The reaction scheme for the simulation model could be simplified.

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“…In addition, the mass transfer in the reactor is also studied. As a result, the kinetic parameters of different studies and different reactors seem very inconsistent with one another and relevant adjustment should be made per specific conditions of utilization. Fortunately, in fluidized‐bed reactors or entrained gasifiers of a sufficiently high temperature, the influence of thermodynamics factors on the reaction process is much greater than kinetic factors.…”

Section: Equivalent Reactor Model Setupmentioning

confidence: 99%

Influence of ash agglomerating fluidized bed reactor scale‐up on coal gasification characteristics

et al. 2014

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To study the influence of fluidized-bed reactor scale-up on coal gasification characteristics, a model of the ash agglomerating fluidized-bed reactor has been developed using an equivalent reactor network method. With the reactor network model, the scale-up effects of a gasifier were studied in terms of the characteristics of the chemical reactions in the jet zone, the annulus dense-phase zone and the freeboard zone. Results showed that the changes occurred in the inequality proportion of the volume of the jet zone during the reactor scale-up. Taking into consideration the utilization of a portion of the backflow gas, the expansion of the jet zone volume and the coal particle residence time, the temperature of the jet zone was increased from 1592 to 1662 K. Also, both the annulus dense-phase zone temperature and the freeboard zone temperature decreased, causing subsequent decrease in the carbon conversion efficiency.

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Mathematical Model for the Gasification of Coal under Pressure

Cited by 137 publications

References 3 publications

Biomass Steam Gasification with In-Situ CO2 Capture for Enriched Hydrogen Gas Production: A Reaction Kinetics Modelling Approach

Biomass Steam Gasification with In-Situ CO2 Capture for Enriched Hydrogen Gas Production: A Reaction Kinetics Modelling Approach

Screening of Kinetic Rate Equations for Gasification Simulation Models

Influence of ash agglomerating fluidized bed reactor scale‐up on coal gasification characteristics

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