Model and Calculation of the Gasification of a Single Carbon Particle

Samuilov, E. V.; Faminskaya, M.V.; Golovina, E. S.

doi:10.1023/b:cesw.0000013670.94694.38

Cited by 16 publications

(8 citation statements)

References 12 publications

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“…The presence of these combustible species contributes to the production of a medium to high heating value gas, suitable for further exploitation in internal combustion engines (ICE) and turbines for power production. LHV calculation was made using the following equation [32]…”

Section: Producementioning

confidence: 99%

Simulation of Olive Kernel Gasification in a Bubbling Fluidized Bed Pilot Scale Reactor

Michailos¹,

Zabaniotou²

2012

JSBS

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The main aim of this study is to develop a comprehensive process model for biomass gasification in a pilot scale bubbling fluidized bed gasifier using the ASPEN PLUS simulator. A drawback in using ASPEN PLUS is the lack of a library model to simulate fluidized bed unit operation. However, it is possible for users to input their own models, using FORTRAN codes nested within the ASPEN PLUS input file, to simulate operation of a fluidized bed. The products of homogeneous reactions are defined by Gibbs equilibrium and reaction rate kinetics are used to determine the products of char gasification. Governing hydrodynamic equations for a bubbling bed and kinetic expressions for the char combustion were adopted from the literature. Different sets of gasification results for the operation conditions (temperature and air equivalence ratio (ER)) obtained from the our pilot-scale gasifier having a capacity of 1 kg/hr of olive kernel as feeding biomass, were used to demonstrate the validation of the model. The simulation results received from the application of the model were compared with the above experimental results and showed good agreement.

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Section: Producementioning

confidence: 99%

Simulation of Olive Kernel Gasification in a Bubbling Fluidized Bed Pilot Scale Reactor

Michailos¹,

Zabaniotou²

2012

JSBS

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“…The diffusion coefficient of oxygen in the H 2 O/O 2 fluid was calculated by the empirical formula proposed in [33]: D [cm 2 /sec] = 2.24 × 10 −6 T 0.792 /ρ, where ρ [g/cm 3 ] is the fluid density and T [K] is the temperature. Theory of the carbon particle porous structure and the penetration dynamics of gas reactants through it has been the subject of extensive studies (see, for example, the bibliography in [34]). In our case, the oxygen flow from the surface of the ash residue to the surface of the unreacted part of the organic matter is conserved and, under the assumption of one-dimensional radial mass transfer, it can be written as follows [35]:…”

Section: Coal Particle Oxidation With Oxygen In a H 2 O/o 2 Fluidmentioning

confidence: 99%

Oxidation of a coal particle in flow of a supercritical aqueous fluid

Vostrikov

Dubov

Psarov

et al. 2008

Combust Explos Shock Waves

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A study was made of the conversion of single spherical coal particles of diameter 1-5 mm in a supercritical H 2 O/O 2 fluid with an oxygen mass fraction of 0-6.6% in a semibatch reactor at a pressure of 30 MPa and a temperature of 673-1023 K. A decrease in the particle mass was observed in two parallel processes: gasification of coal with water and oxidation of coal with oxygen. An activation energy 19 ± 7 kJ/mole and a pre-exponential factor 10 −2±0.4 sec −1 were obtained under the assumption of zero order for the concentration H 2 O and an Arrhenius dependence for the rate of gasification with water. The oxidation with oxygen at a temperature above 780 K was found to be limited by the rate of O 2 diffusion to the coal organic matter. Below 780 K, the rate of heterogeneous oxidation with oxygen is described by a first-order reaction for the concentration of O 2 and a zero-order reaction for the concentration of H 2 O with an activation energy of 150 ± 27 kJ/mole and a pre-exponential factor of 10 7.6±1.9 cm 3 /(g · sec).

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“…The coal conversion process consists of a fast devolatilization phase (which includes particle drying during heat-up) followed by a slower char gasification/combustion phase. Single particle char conversion can be modeled using transient zero dimensional models (which have no spatial discretization), which is done by Samuilov et al [1], for example, and elsewhere [2,3]. Recently Qiao et al (2012) [4] have taken this approach a step further by accounting not only for a single particle but for the effect of a cloud of particles on the gas phase temperature.…”

Section: Introductionmentioning

confidence: 99%

A comprehensive model for char particle conversion in environments containing O2 and CO2

Haugen

Mitchell

Tilghman

2015

Combustion and Flame

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In this work, conversion of char is studied in a simulation code that includes a simplified heterogeneous adsorption-desorption reaction mechanism for char chemical reactivity and uses GRI-Mech 3.0 as the chemical kinetic mechanism that describes the impact of homogeneous reactions. Besides sub-models for the consequences of chemical reactions, a mode of char particle conversion sub-model is included that describes how particle size and apparent density vary with mass loss as well as a radiation sub-model that describes the radiant exchange of energy between the char particle and surrounding particles and walls. The code is transient and zero dimensional in space, and designed to be used both as a stand-alone gasification/combustion code and as a sub-model for heterogeneous reactions of solid particles in a CFD code.

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Model and Calculation of the Gasification of a Single Carbon Particle

Cited by 16 publications

References 12 publications

Simulation of Olive Kernel Gasification in a Bubbling Fluidized Bed Pilot Scale Reactor

Simulation of Olive Kernel Gasification in a Bubbling Fluidized Bed Pilot Scale Reactor

Oxidation of a coal particle in flow of a supercritical aqueous fluid

A comprehensive model for char particle conversion in environments containing O2 and CO2

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