Effect of the blend ratio on the co-gasification of biomass and coal in a bubbling fluidized bed with CFD-DEM

Chen, Juhui; Zhong, Shengliang; Li, Dan; Zhao, Chenxi; Han, Chang-Liang; Yu, Guangbin; Song, Meiqi

doi:10.1016/j.ijhydene.2022.05.075

Cited by 9 publications

(5 citation statements)

References 22 publications

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“…Because this phase does not occur in the start-up phase fluidization behavior, it is at this time that the flow regime in the particle bed changes from the original turbulent fluidization to slugging fluidization. In addition, after 1, 4, and 6 s in Figure a and after 3 and 5 s in Figure c, the same bubble shape is captured, and the particle–particle collisions will be more severe than in the start-up phase . It is worth noting that the inlet flow rate exerts a large influence on the bed height and bubble diameter.…”

Section: Resultssupporting

confidence: 85%

“…In addition, after 1, 4, and 6 s in Figure 7 a and after 3 and 5 s in Figure 7 c, the same bubble shape is captured, and the particle–particle collisions will be more severe than in the start-up phase. 39 It is worth noting that the inlet flow rate exerts a large influence on the bed height and bubble diameter. Especially at the initial stage, the bubble area, the bed height, and the time required to enter the slugging fluidization are positively correlated with the inlet flow rate.…”

Section: Resultsmentioning

confidence: 99%

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Effects of Particle Diameter and Inlet Flow Rate on Gas–Solid Flow Patterns of Fluidized Bed

et al. 2023

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The complex multiscale characteristics of particle flow are notoriously difficult to predict. In this study, the evolution process of bubbles and the variation of bed height were investigated by conducting high-speed photographic experiments to verify the reliability of numerical simulations. The gas–solid flow characteristics of bubbling fluidized beds with different particle diameters and inlet flow rates were systematically investigated by coupling computational fluid dynamics (CFD) and discrete element method (DEM). The results show that the fluidization in the fluidized bed will change from bubbling fluidization to turbulent fluidization and finally to slugging fluidization, and the conversion process is related to the particle diameter and inlet flow rate. The characteristic peak is positively correlated with the inlet flow rate, but the frequency corresponding to the characteristic peak is constant. The time required for the Lacey mixing index (LMI) to reach 0.75 decreases with increasing inlet flow rate; at the same diameter, the inlet flow rate is positively correlated with the peak of the average transient velocity; and as the diameter increases, the distribution of the average transient velocity curve changes from “M” to linear. The results of the study can provide theoretical guidance for particle flow characteristics in biomass fluidized beds.

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Section: Resultssupporting

confidence: 85%

Section: Resultsmentioning

confidence: 99%

Effects of Particle Diameter and Inlet Flow Rate on Gas–Solid Flow Patterns of Fluidized Bed

et al. 2023

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“…The accuracy of the CFD model prediction of the chemical reaction performance was verified with the data obtained by Songip et al 35 The distributions of the reactant and products for various time factors at a temperature of 673 K are depicted in Fig. 2 .…”

Section: Resultssupporting

confidence: 72%

“…These two approaches are the effective methods that currently used to predict gas-solid multiphase ow behaviors coupled with chemical reaction, heat and mass transfer. [34][35][36][37][38][39][40] However, the latter is widely used due to its simplicity and relatively low computational cost. In addition, several researchers applied the CFD approach to simulate FCC in uidized bed reactors.…”

Section: Introductionmentioning

confidence: 99%

Scaling of catalytic cracking fluidized bed downer reactor based on CFD simulations—Part II: effect of reactor scale

et al. 2022

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“…Despite these disadvantages, fluidization has achieved widespread industrial application in many spheres, especially in the chemical and petrochemical industries. It is used for many non-catalytic processes, such as efficient fuel combustion [21], roasting of ores [22], drying [23], adsorption [24], coating [25], granulation [26], etc., but it has become most widespread in the petrochemical industry in a number of catalytic processes, such as the cracking [27] and reforming of hydrocarbons [28], carbonation [29] and coal gasification [30], Fischer-Tropsch synthesis [31], pyrolysis (including pyrolysis of biomass) [32], and hydrogenation and dehydrogenation of hydrocarbons [12][13][14]20,33,34]. A large range of processes based on fluidization and the features of their development and application are presented in the monograph [3].…”

mentioning

confidence: 99%

Numerical Simulation of Hydrodynamics and Heat Transfer in a Reactor with a Fluidized Bed of Catalyst Particles in a Three-Dimensional Formulation

Ulitin,

Tereshchenko,

Rodionov

et al. 2024

Applied Sciences

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The hydrodynamics and heat transfer in a reactor with a fluidized bed of catalyst particles and an inert material were simulated. The particle bed (the particle density was 2350 kg/m3, and the particle diameter was 1.5 to 4 mm) was located in a distribution device which was a grid of 90 × 90 × 60 mm vertical baffles. The behavior of the liquefying medium (air) was modeled using a realizable k-ε turbulence model. The behavior of particles was modeled using the discrete element method (DEM). In order to reduce the slugging effect, the particles were divided into four separate horizontal layers. It was determined that with the velocity of the liquefying medium close to the minimum fluidization velocity (1 m/s), slugging fluidization is observed. At a velocity of the liquefying medium of 3 m/s, turbulent fluidization in the lowest particle layer and bubbling fluidization on subsequent particle layers are observed. With an increase in the velocity of the liquefying medium over 3 m/s, entrainment of particles is observed. It was shown that a decrease in the density of the liquefying medium from 1.205 kg/m3 to 0.383 kg/m3 when it is heated from 298 K to 923 K would not significantly affect the hydraulic resistance of the bed. Based on the obtained results, it can be stated that the obtained model is optimal for such problems and is suitable for the further description of experimental data.

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Effect of the blend ratio on the co-gasification of biomass and coal in a bubbling fluidized bed with CFD-DEM

Cited by 9 publications

References 22 publications

Effects of Particle Diameter and Inlet Flow Rate on Gas–Solid Flow Patterns of Fluidized Bed

Effects of Particle Diameter and Inlet Flow Rate on Gas–Solid Flow Patterns of Fluidized Bed

Scaling of catalytic cracking fluidized bed downer reactor based on CFD simulations—Part II: effect of reactor scale

Numerical Simulation of Hydrodynamics and Heat Transfer in a Reactor with a Fluidized Bed of Catalyst Particles in a Three-Dimensional Formulation

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