Kinetics of coal gasification

Schmal, Martín; Monteiro, J.L.F.; Castellan, Jorge Luiz

doi:10.1021/i200017a008

Cited by 56 publications

(36 citation statements)

References 4 publications

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“…In general, the SC model presented the best fitting, which is a reasonable result, since the gasification is usually classified as an irreversible gas-solid reaction. A similar behavior has been reported in the literature for the gasification of Brazilian coal chars (Schmal et al, 1982;José, 1989;Collazzo, 2013;Domenico, 2013). Although in this work the SC model suitably described the experimental data, it is remarkable that V and RP models presented a good fitting, mainly in the lower temperature and higher temperature ranges, respectively.…”

Section: Application Of Kinetic Modelssupporting

confidence: 85%

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Steam Gasification of a Brazilian Subbituminous Coal Aiming the Production of Syngas

Domenico¹,

José²,

Moreira³

2015

Anais Do XX Congresso Brasileiro De Engenharia Química

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-The aim of this work was to investigate the gasification of a Brazilian low-rank coal in the temperature range of 1023-1198 K and steam concentration range of 10-40% in order to evaluate the reaction rate and the product gas composition. Prior to the gasification experiments the raw coal was pyrolysed in a tubular reactor, under N 2 atmosphere and at a temperature of 1173 K. The coal and char samples were characterized by several techniques. The gasification experiments were performed in a thermobalance, at atmospheric pressure and isothermal conditions. The reactivity study was conducted in the kinetically controlled regime, three theoretical models were tested to fit the experimental data and the kinetic parameters were determined. It was found that an increase in temperature and steam concentration enhances the reaction rate and also the formation of H 2 , CO and CO 2 . The gasification kinetics was suitably described by the Shrinking Core Model and an activation energy of 158 kJ/mol and a reaction order of 0.78 (related to the steam composition) were found. The H 2 /CO ratio remained nearly constant, about 3.0, in all gasification experiments.

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Section: Application Of Kinetic Modelssupporting

confidence: 85%

“…Moreover, information about coals from the South American continent, especially Brazilian coals, is scarce in the literature (Schmal et al, 1982;José, 1989;Collazzo, 2013;Domenico, 2013). Despite the accomplished progress so far, it is still not possible to use data from a particular coal char to predict the behavior of others.…”

Section: Introductionmentioning

confidence: 99%

Steam Gasification of a Brazilian Subbituminous Coal Aiming the Production of Syngas

Domenico¹,

José²,

Moreira³

2015

Anais Do XX Congresso Brasileiro De Engenharia Química

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“…Several studies conducted in the 1980s addressed the kinetics of coal gasification in Brazil (Schmal et al, 1982;José, 1989). For instance, Schmal et al (1982) studied the kinetics of coal gasification between the temperatures of 1073 K and 1273 K with a high-ash coal from southern Brazil.…”

Section: Brazilian Journal Of Chemical Engineeringmentioning

confidence: 99%

“…For instance, Schmal et al (1982) studied the kinetics of coal gasification between the temperatures of 1073 K and 1273 K with a high-ash coal from southern Brazil. The authors determined that the unreacted core model fit the results up to a temperature of 1123 K and that the continuous reaction model was optimal above this temperature.…”

Section: Brazilian Journal Of Chemical Engineeringmentioning

confidence: 99%

Determination of the Kinetic Parameters of Oxy-Fuel Combustion of Coal With a High Ash Content

Nunes

Marcílio

2015

Braz. J. Chem. Eng.

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-The aim of this study was to determine the kinetic parameters of the oxy-fuel combustion of char from a Brazilian bituminous coal with a high ash content. The char, with a particle diameter of 715 μm, was prepared in a N 2 atmosphere at 1173 K. The oxy-fuel combustion assays were performed using a thermobalance at different temperatures and O 2 /CO 2 gas mixtures of different concentrations. According to the unreacted core model, the process is determined by chemical reaction at low temperatures, with an activation energy of 56.7 kJ.kmol -1 , a reaction order of 0.5 at 973 K and a reaction order of 0.7 overall. The use of the continuous reaction model did not provide a good fit for the experimental data because the consumption of the particles during the reaction was not constant, as predicted by the model. According to the Langmuir-Hinshelwood model, the activation energy for the first step was 37.3 kJ.kmol -1 .

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“…These results are consistent with these published in the literature. So, as an example, Schmal et al 20 concluded that the diffusion and thermal effect are negligible when the height bed/particle diameter ratio is equal to or lower than 2, which led them to employ initial masses lower than 0.7 g in their experimental system.…”

Section: Non-catalytic Gasification: Influence Of Variablesmentioning

confidence: 99%

Catalyzed gasification of active carbon by oxygen: influence of catalyst type, temperature, oxygen partial pressure and particle size

Martín

González

Sabio

et al. 2000

J. Chem. Technol. Biotechnol.

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A thermogravimetric study of the oxygen gasi®cation of a commercial active carbon using Co, Ni and Cu as catalysts has been carried out. This follows a previous study of the in¯uence of the particle size, gas volumetric¯ow rate, initial sample weight temperature and oxygen partial pressure an non-catalytic gasi®cation. The results show that for T`500°C; P 02`1 atm; D p`0 .4 mm, Q v b 50 cm 3 min À1 and M o`7 5 mg the gasi®cation of the active carbon with oxygen is controlled by the chemical reaction. The presence of a catalyst increases in all cases the reaction rate, both temperature and catalyst concentration showing a very positive in¯uence. The activity of the different catalysts follows the order: Co b Cu b Ni. A kinetic study applied to both types of gasi®cation has allowed the activation energy and the reaction order with respect to oxygen and the catalyst to be determined. In all cases both the activation energy and the Arrhenius pre-exponential factor are lower in the catalytic gasi®cation. This brings about the existence of an isokinetic point for the catalytic and the non-catalytic processes, which were also determined.

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Kinetics of coal gasification

Cited by 56 publications

References 4 publications

Steam Gasification of a Brazilian Subbituminous Coal Aiming the Production of Syngas

Steam Gasification of a Brazilian Subbituminous Coal Aiming the Production of Syngas

Determination of the Kinetic Parameters of Oxy-Fuel Combustion of Coal With a High Ash Content

Catalyzed gasification of active carbon by oxygen: influence of catalyst type, temperature, oxygen partial pressure and particle size

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