Main entry under title: Gas fluidization technology. ‘A Wiley-Interscience publication.’ Includes index. 1. Fluidization. I. Geldart, D, TPF65G37 ISBN 0. permission of the publisher. Gas fluidization technology. ‘A Wiley-Interscience publication.’ Includes index. 1. Fluidization. I. Geldart, D, TPF65G37 Powder Technology The behaviour of solids fluidized by gases falls into four clearly recognizable groups, characterized by density difference (ϱs–ϱf) and mean D. Geldart. Powder Technol., 6 (), p. 2. R.H. Wilhelm, M. Kwauk .

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A partial listing of these probes appears in Table These problems arise from transfer of gas between separate bubbles through the permeable intervening dense phase.

Clearly slugs can only exist if the diameter of the largest bubble is greater than q. For coarse, very angular, or cohesive particles, ‘plug’ flow occurs in beds of much larger diameter and is suppressed by roughening the walls Geldart, Hurt, and Wadia, PI kglm3 This is consistent with observations see Chapter 3.

This involves passing air or water at a known velocity upwards through a powder sample anti! Introduction by Geldart 2. Yang and Keairns reviewed the correlations available for predicting the length of the ‘jet’ established when gas enters a fluidized bed vertically, concluded that none was sufficiently general, and proposed their own: The fluidization literature is so enormous and so many new papers and patents are published every year Geldart, that it is difficult for the specialist to keep up – let alone for the novice to gain a good perspective.

Particle Size Measurement, 3rd ed.

Under such circumstances the tube surface temperature may approximate to to oe, leading to an apparent emissivity of about 0. Total pressure drop contribution. The material collected is weighed and its size calculated using Stokes’ law.


Fundamentals of Fluidized-bed Chemical Processes, Butterworths. Under laminar flow conditions Re H d;v e Vs where Ys is positive if the particles move in the same direction as the gas or is negative if they move counter-current.

Gas Fluidization Technology

They found experimentally that several different flow regimes are possible and that the flow regimes could be predicted with their mathematical model. In addition, a number of workers have avoided probe interference effects by affixing capacitance plates to opposite walls of experimental columns. Corresponding to each data point, the figures also display the fluidized density reckoned from the mean pressure drop across the bed and the bed depth.

At Reynolds numbers less than about 1 laminar flow the Carman-Kozeny equation applies: Somewhat larger gap widths are required for angular particles or for powders having broad size distributions. However, it has been pointed out by Zabrodsky that a particulate bed will have a different overall emissivity to that of its constituent material.

Calculate UTQ from Eq.

There are probably more fluid beds used as dryers than any other single application geldarrt their design is outlined in Chapter There are few, if any mistakes. However, the values obtained are generally consistent with those inferred by Grace. Calculate terminal velocity for particles: Because conversion takes place continuously, thus gradually reducing the density of the limestone, there will be relatively little pure limestone in the bed.

Gas Fluidization Technology Edited by. Students and researchers in the broader field of chemical engineering should also find topics of interest here. The capacitance of a region therefore depends on the concentration of solid particles texhnology that region. Bubble rise velocity fluidkzation calculated from Eq. However, correspondence was very close between measured and predicted values when using a calorimetric exchange surface of much higher heat capacity.

A reasonable value for gs for Eapp would be 0. Abrahamsen found that for fine powders of mean size 30 to 80! This effect could be expected, for example, to increase the heat transfer rate to crushed coal as it is charged to a fluidized bed combustor above that predicted by the simple correlation. The tracking method developed recently by Lin, Chen, and Chao is also very powerful, but requires multiple detectors and sophisticated and extensive data storage and processing facilities.


If this type of bend is present in a system, it is possible for solids to remain on the bottom of the pipe for very long distances following the bend, before they hechnology Fig. Bends complicate the design of pneumatic dilute phase transfer systems, and when designing a conveying system it is best to use as few bends as possible. Thesis, University of Fluidizahion.

Gas fluidization technology ( edition) | Open Library

In the first, attrition of valuable catalyst in cyclones and loss of the fines can increase the cost and controllability of the operation; in the second the solids are a coarse sand which remains in the bed, and the fine light ash from the burnt sludge is carried out continuously as an overhead product, thus providing a convenient method of removal; in the third process, high throughput and the control of residence time and bed temperature depend on achieving high carryover rates.

Although this is to be discussed in detail in Chapter 3 a simplified version is shown in Fig.

Results have been expressed by means of stimulus-response curves, diffusion-type models, and a variety of more or less sophisticated two-region models. The bed expands, apparently smoothly and homogenously, until a velocity is reached at which 2.