Riser hydrodynamic study with different Group B powders

Experiments were conducted in a large cold flow CFB unit (18 m long riser and 30 cm in diameter) with three Group B powders. Sand, glass beads and a metal ore, with similar particle size, were used to study the impact of particle density and sphericity. The impact of particle nature on the riser hydrodynamics was investigated at similar operating conditions. Resulting axial pressure profiles are very different in both the acceleration and the fully developed region. These differences can most probably be explained by the difference in shape between the solids. Higher sphericity seems to generate less pressure drop and smaller values of drag force. The influence of particle shape on acceleration resulting fromgas–solidmomentumtransfer and the impact on particle concentration in the fully developed region are then studied. To analyze the results, amonodimensionalmomentumbalance study was conducted, resulting in a new formulation for the average drag force, based on experimental results.

[1]  John R. Grace,et al.  Circulating fluidized beds , 1996 .

[2]  John D. Paccione,et al.  Modeling and measurement of the effective drag coefficient in decelerating and non-accelerating turbulent gas—solids dilute phase flow of large parti , 1993 .

[3]  H. Weinstein,et al.  An evaluation of the actual density in the acceleration section of vertical risers , 1989 .

[4]  Shozaburo Saito,et al.  PNEUMATIC CONVEYING OF SOLIDS THROUGH STRAIGHT PIPES , 1969 .

[5]  Mingchuan Zhang,et al.  Hydrodynamics of gas-solid flow in the circulating fluidized bed reactor for dry flue gas desulfurization , 2011 .

[6]  Jamal Chaouki,et al.  Effective drag coefficient investigation in the acceleration zone of an upward gas–solid flow , 2007 .

[7]  Jesse Zhu,et al.  Effects of particle properties on flow structure in a 2-D circulating fluidized bed: Solids concentration distribution and flow development , 2011 .

[8]  Jesse Zhu,et al.  Scale-up effect of riser reactors (3) axial and radial solids flux distribution and flow development , 2005 .

[9]  Poupak Mehrani,et al.  Investigation of electrostatic charge distribution in gas–solid fluidized beds , 2010 .

[10]  Franco Berruti,et al.  Evaluation of the gas–solid suspension density in CFB risers with exit effects , 2000 .

[11]  Jamal Chaouki,et al.  Scaling considerations for circulating fluidized bed risers , 1992 .

[12]  J. You,et al.  Modeling of core flow in a gas–solids riser , 2010 .

[13]  Mohammad. M. Hossain,et al.  Chemical-looping combustion (CLC) for inherent CO2 separations—a review , 2008 .

[14]  Atsushi Tsutsumi,et al.  Effects of solids feeder and riser exit configuration on establishing high density circulating fluidized beds , 2008 .

[15]  Efstathios E. Michaelides,et al.  Drag coefficients of irregularly shaped particles , 2004 .

[16]  M. Yazdanpanah,et al.  An experimental investigation of loop-seal operation in an interconnected circulating fluidized bed system , 2012 .

[17]  Sofiane Benyahia,et al.  A time-averaged model for gas–solids flow in a one-dimensional vertical channel , 2008 .

[18]  Chi‐Hwa Wang,et al.  Electrostatic characteristics in a large-scale triple-bed circulating fluidized bed system for coal gasification , 2012 .

[19]  D. Geldart Types of gas fluidization , 1973 .

[20]  Electrostatics in gas–solid fluidized beds for different particle properties , 2012 .

[21]  Yong Jin,et al.  Investigation on slip velocity distributions in the riser of dilute circulating fluidized bed , 1992 .

[22]  C. Hrenya,et al.  Cluster characteristics of Geldart group B particles in a pilot-scale CFB riser. II. Polydisperse systems , 2012 .

[23]  O. Levenspiel,et al.  Drag coefficient and terminal velocity of spherical and nonspherical particles , 1989 .

[24]  M. Yazdanpanah Investigation of a Chemical Looping Combustion (CLC) Configuration with Gas Feed , 2011 .

[25]  Jia Wei Chew,et al.  Reverse core-annular flow of Geldart Group B particles in risers , 2012 .