Table 7: Results obtained from the semiempirical model.

RiserParticle terminal velocity corrected by sphericity, 3.04 m/s
Superficial gas velocity, 5.54 m/s
Solids circulation flux in the riser, 20.93 kg/m2·s
Choking voidage, 0.9969
Voidage fraction at the riser exit, 0.9962
Riser height, H 4.00 m
Riser height-to-internal diameter ratio, 39.2
Solids inventory in the total riser height, 3.52 kg
Pressure drop in the total riser height, 4,268 Pa
Solids return level above the riser base 0.45 m
Pressure drop in the riser measured above the solids return level, 3,077 Pa

CycloneVolumetric gas flow entering the cyclone, Q 0.045 m/s
Solid-to-gas mass ratio at the cyclone entrance, 3.8
Gas velocity at the inlet section of the cyclone, 14.83 m/s
Cyclone dimensions [m]:
Dc = 0.182; A = 0.080; C = 0.038; M = 0.073; F = 0.091; S = 0.255; B = 0.709; .
Gas velocity at the cyclone exit, 10.90 m/s
Pressure drop in the cyclone, 271 Pa

Standpipe and L-valveInternal diameter of the standpipe and the L-valve, 0.063 m
Circulating solids flux in the standpipe and the L-valve, 55.2 kg/m2·s
Solids velocity in the moving bed, 0.04 m/s
Horizontal section of the L-valve, 0.36 m
Aeration level above of the horizontal section center line, 0.13 m
Aeration mass flow rate in the L-valve, 1.97 kg/h
Height of the solids above the aeration point, 0.50 m
Height of the standpipe, 2.71 m
Pressure drop in the L-valve, 3,917 Pa
Pressure drop in the standpipe, 7,265 Pa

Total solids inventory in the CFB system8.20 kg