Heat transfer between fluidized beds of large particles and horizontal tube bundles at high pressures

1984 ◽  
Vol 27 (8) ◽  
pp. 1219-1225 ◽  
Author(s):  
V.A. Borodulya ◽  
V.L. Ganzha ◽  
A.I. Podberezsky ◽  
S.N. Upadhyay ◽  
S.C. Saxena
Keyword(s):  
Heat Transfer ◽  
Fluidized Beds ◽  
High Pressures ◽  
Horizontal Tube ◽  
Large Particles ◽  
Tube Bundles

Heat-transfer from horizontal tube bundles into fluidized beds with Geldart A lignite particles

2014 ◽  
Vol 253 ◽  
pp. 14-21 ◽  
Author(s):  
Stefan Lechner ◽  
Matthias Merzsch ◽  
Hans Joachim Krautz
Keyword(s):  
Heat Transfer ◽  
Fluidized Beds ◽  
Horizontal Tube ◽  
Tube Bundles

Heat transfer between gas-solid fluidized beds and horizontal tube bundles

1980 ◽  
Vol 7 (2) ◽  
pp. 83-95 ◽  
Author(s):  
V.A. Borodulya ◽  
V.L. Ganzha ◽  
A.I. Zheltov ◽  
S.N. Upadhyay ◽  
S.C. Saxena
Keyword(s):  
Heat Transfer ◽  
Fluidized Beds ◽  
Horizontal Tube ◽  
Tube Bundles

Artificial Neural Network Based Prediction of Heat Transfer From Horizontal Tube Bundles Immersed in Gas–Solid Fluidized Bed of Large Particles

2014 ◽  
Vol 137 (1) ◽  
Author(s):  
L. V. Kamble ◽  
D. R. Pangavhane ◽  
T. P. Singh
Keyword(s):  
Neural Network ◽  
Heat Transfer ◽  
Artificial Neural Network ◽  
Fluidized Bed ◽  
Particle Diameter ◽  
Horizontal Tube ◽  
Feed Forward Network ◽  
Large Particles ◽  
Tube Bundles ◽  
Artificial Neural

Artificial neural network (ANN) modeling of heat transfer from horizontal tube bundles immersed in gas fluidized bed of large particles (mustard, raagi and bajara) was investigated. The effect of fluidizing gas velocity on the heat transfer coefficient in the immersed tube bundles in in-line and staggered arrangement is discussed. The parameters particle diameter, temperature difference between bed and immersed surface were used in the neural network (NN) modeling along with fluidizing velocity. The feed-forward network with back propagation structure implemented using Levenberg–Marquardt's learning rule in the NN approach. The predictions of the ANN were found to be in good agreement with the experiment's values, as well as the results achieved by the developed correlations.

High pressure heat transfer investigations for fluidized beds of large particles and immersed vertical tube bundles

1983 ◽  
Vol 26 (11) ◽  
pp. 1577-1584 ◽  
Author(s):  
V.A. Borodulya ◽  
V.L. Ganzha ◽  
A.I. Podberezsky ◽  
S.N. Upadhyay ◽  
S.C. Saxena
Keyword(s):  
Heat Transfer ◽  
High Pressure ◽  
Fluidized Beds ◽  
Vertical Tube ◽  
Large Particles ◽  
Tube Bundles

Heat transfer around a horizontal tube in freeboard region of fluidized beds

AIChE Journal ◽  
1983 ◽  
Vol 29 (5) ◽  
pp. 712-716 ◽  
Author(s):  
S. Biyikli ◽  
K. Tuzla ◽  
J. C. Chen
Keyword(s):  
Heat Transfer ◽  
Fluidized Beds ◽  
Horizontal Tube

Heat Transfer in Large Particle Bubbling Fluidized Beds

1984 ◽  
Vol 106 (1) ◽  
pp. 85-90 ◽  
Author(s):  
R. L. Adams
Keyword(s):  
Heat Transfer ◽  
Experimental Data ◽  
Residence Time ◽  
Large Particle ◽  
Fluidized Beds ◽  
Horizontal Tube ◽  
Two Dimensional ◽  
Phase Contact ◽  
Emulsion Phase ◽  
Bubble Phase

The potential use of fluidized bed combustion of coal as a means of meeting air quality standards with high-sulfur fuels has motivated the development of theoretical models of heat transfer in large particle gas fluidized beds. Models of the separate contributions of emulsion and bubble phase heat transfer have been developed by Adams and Welty [1] and Adams [2, 3, 4] and have been substantiated by experimental data for a horizontal tube immersed in a two-dimensional cold bed obtained by Catipovic [5, 6]. The consolidation of these models to predict local and overall time-average heat transfer to immersed surfaces requires information regarding emulsion phase residence time and bubble phase contact fraction for the particular geometry of interest. The analytical procedure to consolidate these models is outlined in the present work, then applied to the case of a horizontal tube immersed in a two-dimensional atmospheric pressure cold bed. Measurements of emulsion phase residence time and bubble phase contact fraction obtained by Catipovic [5] are used in the calculations for particle diameters ranging from 1.3 to 6 mm. The results agree favorably with experimental data and further substantiate the fundamental assumptions of the model.

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