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Research Papers: Multiphase Flows

CFD Simulation of the Bubbling and Slugging Gas-Solid Fluidized Beds

[+] Author and Article Information
Seyyed Hossein Hosseini1

Department of Chemical Engineering, Faculty of Engineering, University of Ilam, Ilam, Irans.h.hosseini@mail.ilam.ac.ir

Wenqi Zhong

School of Energy and Environment, Southeast University, Nanjing 210096, People’s Republic of China

Mohsen Nasr Esfahany

Department of Chemical Engineering, Isfahan University of Technology, Isfahan 8415683111, Iran

Leila Pourjafar

Department of Chemical Engineering, University of Sistan and Baluchesta, Zahedan 98164-161, Iran

Salar Azizi

Department of Chemical Engineering, Faculty of Engineering, Arak University, Arak, Iran

1

Corresponding author.

J. Fluids Eng 132(4), 041301 (Mar 29, 2010) (10 pages) doi:10.1115/1.4001140 History: Received June 25, 2009; Revised January 18, 2010; Published March 29, 2010; Online March 29, 2010

A two-dimensional transient Eulerian model integrating the kinetic theory for emulsion phase is used to simulate the bubbling and slugging gas-solid fluidized beds, including the Geldart B and D particles, respectively. CFD results show that utilizing an algebraic granular temperature equation, instead of a full granular temperature, one leads to a significant reduction in computational time without loosing accuracy. Different drag models have been examined in the current study. CFD results show that the Syamlal–O’Brien and Di Felice adjusted drag models, based on minimum fluidization velocity, are not suitable for the bed, including coarse particles (Geldart group B). The Gidaspow drag model displays better results in comparison with the others. A good agreement with the available experimental data and the researcher’s findings has been reached quantitatively and qualitatively. The proposed model can reasonably be used for simulation of slugging fluidized beds. This study reduces the computational error compared with the previous works.

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Copyright © 2010 by American Society of Mechanical Engineers
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References

Figures

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Figure 1

Time-averaged solid volume fraction along the bed height using PDE and algebraic equation of granular temperature

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Figure 2

Quantitatively comparison between different drag models at wide range of solid volume fraction

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Figure 3

Computed bed expansion ratio by using different drag models compared with experimental data

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Figure 4

Comparison of experimental and simulated time-averaged local voidage using different drag models at y=0.2 m and Ug=0.38 m/s

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Figure 5

Comparison of experimental and simulated time-averaged local voidage using drag models of Gidaspow and Syamlal–O’Brien at y=0.2 m and Ug=0.46 m/s

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Figure 6

Comparison of experiment and simulated bubbles for different drag models qualitatively (Ug=0.38 m/s)

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Figure 7

Time-averaged pressure drop against superficial gas velocity (a) inside the bed and (b) overall the bed

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Figure 8

Simulated bed pressure drop versus time at different gas velocities

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Figure 9

Computed time-averaged (a) solid volume fraction and (b) solid axial velocity (m/s)

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Figure 10

Comparison between simulation results and experimental data in terms of radial distribution of gas volume fraction at various axial locations of the bed and Ug=2.8 m/s: (a) computational and (b) experimental

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Figure 11

Time-averaged velocity vectors of particles at Ug=2.8 m/s

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Figure 12

Contour plot of gas volume fraction at Ug=2.8 m/s

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