Particle motion in the CFB riser with special emphasis on PEPT-imaging of the bottom section
Chan, Chian W., Seville, J. P. K. (Jonathan P. K.), Yang, Zhufang and Baeyens, Jan. (2009) Particle motion in the CFB riser with special emphasis on PEPT-imaging of the bottom section. Powder Technology, Vol.196 (No.3). pp. 318-325. ISSN 0032-5910Full text not available from this repository.
Official URL: http://dx.doi.org/10.1016/j.powtec.2009.08.019
The riser is the key-part of a circulating fluidized bed (CFB) and its hydrodynamics are determined mainly by the combined operating superficial gas velocity, U. and solids circulation flux, G. The bottom part of the riser contributes to the total pressure drop of the riser and affects the solids residence time in the riser, due to the possible existence of a dense bed and to the presence of an acceleration zone. Positron Emission Particle Tracking (PEPT) is applied to study these phenomena by measuring the real-time particle motion in a riser of 0.09 m diameter, defining (i) the extent of the acceleration zone, including acceleration length and acceleration time; (ii) the occurrence of a bubbling/turbulent bed under specific conditions of U and G; (iii) the establishment of a fully developed flow immediately after the acceleration zone; (iv) the occurrence of core-annulus flow under specific combinations of U and G: and (v) the disappearance of the intermediate core-annulus region at high values of U and G, where riser hydrodynamics will be either dilute or dense solid upflow. The particle upflow velocity, U-pf. after acceleration was measured and compared with the situation of dilute transport. When the solids circulation flux increases, the dilute transport mode no longer prevails, and U-pf should be calculated using an appropriate slip factor, itself a combined factor of U and G. The acceleration length and time are nearly constant, at an approximate average of 0.26 m and 0.21 s respectively, independent of U and G. The acceleration length can be modelled fairly accurately. using a C-D-factor of approximately 3.2, which is about half the value predicted by empirical equations established for dilute transport. Dense Suspension Upflow (DSU) is achieved when G exceeds similar to 130 kg m(-2) s(-1). (C) 2009 Elsevier B.V. All rights reserved.
|Item Type:||Journal Article|
|Subjects:||T Technology > TP Chemical technology|
|Divisions:||Faculty of Science > Engineering|
|Library of Congress Subject Headings (LCSH):||Positrons -- Emissions, Acceleration (Mechanics), Fluidization, Chemistry, Technical, Chemical engineering|
|Journal or Publication Title:||Powder Technology|
|Publisher:||Elsevier Science SA|
|Date:||22 December 2009|
|Number of Pages:||8|
|Page Range:||pp. 318-325|
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