The relative influence of smooth and abrupt exit configurations on the axial pressure drop profile in Circulating Fluidized Bed (CFB) risers has been investigated. Experiments were performed with sand and FCC catalyst in two cold model CFBs of 0.1 metre and 0.2 metre riser diameter. The influence of the abrupt exit on the profile was observed to extend all the way to the base of the larger diameter riser for sand. However, the abrupt exit influenced only the final 1.5 to 2 metres of the riser length for the case of sand in the narrow diameter riser. When FCC catalyst was circulated, the effect of the abrupt configuration was seen only in the upper portion of the riser, irrespective of the riser diameter. A simple empirical modification to the model of Pugsley and Bermti (1996) provides a good description of the axial pressure drop profiles for the abrupt exit configurations, with the exception of the case of sand in the 0.2 metre diameter riser. This discrepancy is attributed to the lack of fully developed flow in the larger riser.
On a etudie l'influence relative de configuration de sorties douces et abruptes sur le profil de perte de charge axiale dans des colonnes montantes de lits fluidisants circulants (CFB). Les experiences ont ete realisees avec du sable et un catalyseur de FCC dans deux modeles froids de CFB de 0, l mebe et 0.2 mere de diametre de colonne. On a observe que l'influence de la sortie abrupte sur le profil s'etendait jusqu' a la base de la colonne ayant le diametre le plus large pour le sable. Cependant, la sortie abrupte influence seulement les demiers 1.5 m a 2 m de la colonne dans le cas du sable pour ce qui est de la colonne ayant un diametre etroit. Lorsqu'on fait circuler le catalyseur de FCC, l'effet de la configuration abrupte n'est observe que dans la partie superieure de la colonne rnontante, quel que soit le diametre de la colonne. Une modification empirique simple du modele de Pugsley et Bermti (1996) donne une bonne description des profils de perk de charge axiale pour les configurations de sortie abruptes, excepte pour le cas du sable dans la colonne montante de 0.2 metre de diametre. Cette difference est imputee A l'absence d'ecoulement completement developpe dans la colonne la plus large.
[1]
P. Guigon,et al.
A new method for local solid concentration measurement in circulating fluidized bed
,
1996
.
[2]
Gabriel Wild,et al.
Gas and solid behavior in cracking circulating fluidized beds
,
1992
.
[3]
Jam Hans Kuipers,et al.
Measurements of solids concentration and axial solids velocity in gas-solid two-phase flows.
,
1996
.
[4]
Joachim Werther,et al.
SOLIDS CONCENTRATION AND VELOCITY PATTERNS IN CIRCULATING FLUIDIZED BEDS
,
1988
.
[5]
Franco Berruti,et al.
A predictive hydrodynamic model for circulating fluidized bed risers
,
1996
.
[6]
Mooson Kwauk,et al.
The Dynamics of Fast Fluidization
,
1980
.
[7]
T. Shingles,et al.
COMMERCIAL EXPERIENCE WITH SYNTHOL CFB REACTORS
,
1988
.
[8]
Arthur M. Squires,et al.
The Fast Fluidized Bed
,
1976
.
[9]
Jamal Chaouki,et al.
Hydrodynamics of circulating fluidized bed risers: A review
,
1995
.
[10]
T. M. Knowlton,et al.
Gas/solids flow patterns in a 30.5-cm-diameter circulating fluidized bed
,
1988
.
[11]
C.M.H. Brereton,et al.
Modelling of circulating fluidised-bed solids flow and distribution
,
1992
.
[12]
M. Kruse,et al.
2D gas and solids flow prediction in circulating fluidized beds based on suction probe and pressure profile measurements
,
1995
.
[13]
Jamal Chaouki,et al.
Scaling considerations for circulating fluidized bed risers
,
1992
.
[14]
Arthur M. Squires,et al.
THE STORY OF FLUID CATALYTIC CRACKING: THE FIRST “CIRCULATING FLUID BED”
,
1986
.
[15]
Yong Jin,et al.
The axial distribution of the cross-sectionally averaged voidage in fast fluidized beds
,
1992
.