Particle velocity measurements in a circulating fluidized bed

AIChE Journal ◽  
1993 ◽  
Vol 39 (8) ◽  
pp. 1406-1410 ◽  
Author(s):  
T. Wang ◽  
Z. J. Lin ◽  
C. M. Zhu ◽  
D. C. Liu ◽  
S. C. Saxena
Keyword(s):  
Fluidized Bed ◽  
Particle Velocity ◽  
Circulating Fluidized Bed ◽  
Velocity Measurements

scholarly journals Effects of Riser Diameter on Solids Holdup and Particle Velocity Profiles in Circulating Fluidized Bed Riser Systems

2020 ◽  
Vol 142 (7) ◽  
Author(s):  
Ronald W. Breault ◽  
Steven L. Rowan ◽  
Justin M. Weber ◽  
Jingsi Yang
Keyword(s):  
Fluidized Bed ◽  
Particle Velocity ◽  
Circulating Fluidized Bed ◽  
Velocity Profiles ◽  
Small Scale ◽  
Sauter Mean Diameter ◽  
Particle Size Range ◽  
Cold Flow ◽  
Solids Holdup ◽  
Radial Profiles

Abstract Tests were performed in a 0.1-m diameter small circulating fluidized bed (SCFB) and 0.3 m diameter cold flow circulating fluidized bed (CFCFB) riser systems located at the National Energy Technology Laboratory (NETL) to study the effects of riser diameter on the riser hydrodynamics. These tests were performed at solids circulation rates of Gs = 20 and 75 kg/m2 s and superficial gas velocities of Ug = 5.8 and 6.5 m/s using high-density polyethylene (HDPE) pellets with a density of 0.863 g/cm3, particle size range of 600–1400 µm (with a Sauter mean diameter of 871 µm, placing them in the Geldart B classification). Comparisons of riser axial pressure and solids fraction profiles, radial particle velocity profiles, and radial profiles of higher statistical moments and select chaos analysis parameters were considered. The results showed that for a given Ug and Gs, the smaller diameter riser exhibited characteristics associated with more dilute solids flow than that observed in the larger diameter riser. Additionally, the larger diameter riser exhibited a downward flow of solids near the wall under all test conditions, whereas the smaller diameter riser data exhibited little or no indications of solids downflow near the wall. These findings suggest that, from an industrial standpoint, a direct scaleup of small-scale tests cannot readily be accomplished as the solids holdup and the solids velocity profiles in small units (those normally tested in the laboratory) are not similar to those of large units and the performance of large units can therefore not be predicted from small-scale tests.

Particle Velocity Distribution and Its Prediction in a 14 m Two-Dimensional Circulating Fluidized Bed Riser

2021 ◽  
Vol 60 (4) ◽  
pp. 1901-1911
Author(s):  
Chengxiu Wang ◽  
Xiao Yang ◽  
Min Wang ◽  
Jiazhi Zhang ◽  
Xingying Lan ◽  
...  
Keyword(s):  
Velocity Distribution ◽  
Fluidized Bed ◽  
Particle Velocity ◽  
Circulating Fluidized Bed ◽  
Two Dimensional

Image Analysis with Spatial Filtering Method for Fluidizing Particle Velocity in a Circulating Fluidized Bed

1992 ◽  
pp. 740-744 ◽  
Author(s):  
Yasuo Katoh ◽  
Masahide Miyamoto ◽  
Shingo Kaneko ◽  
Hidetoshi Miike ◽  
Kazutoshi Koga
Keyword(s):  
Image Analysis ◽  
Fluidized Bed ◽  
Particle Velocity ◽  
Circulating Fluidized Bed ◽  
Spatial Filtering ◽  
Filtering Method
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