Effect of adjusted mesoscale drag model on flue gas desulfurization in powder-particle spouted beds

doi:10.1007/s11705-021-2100-8

Front. Chem. Sci. Eng.

2022, Vol. 16

Issue (6) : 909-920 https://doi.org/10.1007/s11705-021-2100-8

RESEARCH ARTICLE

Effect of adjusted mesoscale drag model on flue gas desulfurization in powder-particle spouted beds

Xinxin Che, Feng Wu(

), Xiaoxun Ma

School of Chemical Engineering, Northwest University, Xi’an 710069, China

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Abstract

An energy minimum multiscale model was adjusted to simulate the mesoscale structure of the flue gas desulfurization process in a powder-particle spouted bed and verified experimentally. The obtained results revealed that the spout morphology simulated by the adjusted mesoscale drag model was unstable and discontinuous bubbling spout unlike the stable continuous spout obtained using the Gidaspow model. In addition, more thorough gas radial mixing was achieved using the adjusted mesoscale drag model. The mass fraction of water in the gas mixture at the outlet determined by the heterogeneous drag model was 1.5 times higher than that obtained by the homogeneous drag model during the simulation of water vaporization. For the desulfurization reaction, the experimental desulfurization efficiency was 75.03%, while the desulfurization efficiencies obtained by the Gidaspow and adjusted mesoscale drag models were 47.63% and 75.08%, respectively, indicating much higher accuracy of the latter technique.

Keywords adjusted mesoscale drag model particle image velocimetry water vaporization desulfurization reaction numerical simulation

Corresponding Author(s): Feng Wu

Online First Date: 09 December 2021 Issue Date: 28 June 2022

Cite this article:

Xinxin Che,Feng Wu,Xiaoxun Ma. Effect of adjusted mesoscale drag model on flue gas desulfurization in powder-particle spouted beds[J]. Front. Chem. Sci. Eng., 2022, 16(6): 909-920.

URL:

https://academic.hep.com.cn/fcse/EN/10.1007/s11705-021-2100-8
https://academic.hep.com.cn/fcse/EN/Y2022/V16/I6/909

Fig.1 (a) Geometric model and (b) mesh division of the spouted bed (unit: mm).

Tab.1 Physical properties of each phase

Fig.2 Radial particle velocities obtained experimentally and by using different drag models.

Fig.3 Contours of the particle volume fraction obtained at various times using the (a) Gidaspow and (b) EMMS drag models.

Fig.4 Contours of the radial and axial distribution of the gas (a) axial and (b) radial velocities (unit: m?s^–1).

Fig.5 (a) Turbulent dissipation rates and (b) granular temperatures obtained at various radial distances for different drag models and bed heights (z = 0.04, 0.08, and 0.12 m).

Fig.6 Contours of the water vaporization rate obtained for different drag models.

Fig.7 Gas-liquid-solid three-phase temperature plotted as a function of the radial distance for different drag models and bed heights of (a) z = 0.04, (b) z = 0.08, and (c) z = 0.12 m.

Fig.8 Contours of the volume fraction of CaSO₃ desulfurization product obtained for different drag models.

Fig.9 Product generation rate plotted as a function of the radial distance for different drag models and bed heights of 0.04, 0.08, and 0.12 m.

Fig.10 Desulfurization efficiencies obtained by numerical simulations and the related experimental value.

$d pc$	particle diameter, m
$d pf$	sorbent diameter, m
$d cl$	cluster diameter, m
$C D$	particle apparent drag coefficient, dimensionless
$H d$	correction factor, dimensionless
$a$	average acceleration, m?s^–2
$f$	volume fraction of dense phase, dimensionless
$G s$	particle circulation, kg?m^–2?s^–1
$U g$	superficial gas velocity, m?s^–1
$U gc$	superficial gas velocity in dense phase, m?s^–1
$U g f$	superficial gas velocity in dilute phase, m?s^–1
$U mf$	minimum fluidization velocity, m?s^–1
$U p$	superficial particle velocity, m?s^–1
$U pc$	superficial particle velocity in dense phase, m?s^–1
$U pf$	superficial particle velocity in dilute phase, m?s^–1
$U sc$	dense phase superficial slip velocity, m?s^–1
$U sf$	dilute phase superficial slip velocity, m?s^–1
$U si$	inter-phase superficial slip velocity, m?s^–1
$R e$	Reynolds number, dimensionless
$S c$	Schmidt dimensionless number, dimensionless
$Y sat$	vapor mass fraction at gas-liquid interface, dimensionless
$D SO 2, g$	diffusion coefficient of SO₂, _{dimensionless}
$η SO 2$	liquid membrane mass transfer enhancement factor, dimensionless
$H SO 2$	Henry coefficient, dimensionless
x, z	Cartesian coordinates, m
Greek letters
$β$	drag coefficient, kg?m^–2?s^–1
$u g$	gas velocity, m?s^–1
$u p$	particle velocity, m?s^–1
$ρ$	density, kg?m^–3
$μ$	viscosity, kg?m^–1?s^–1
$ε g$	gas voidage, dimensionless
$ε p$	particle voidage, dimensionless
$ε max$	maximum voidage, dimensionless
$ε mf$	voidage at minimum fluidization, dimensionless
Subscripts
g	gas phase
p	particle phase
$i$	inter-phase
c	dense phase
f	dilute phase

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