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TECHNICAL PAPERS

Modeling of Heat Transfer in a Moving Packed Bed: Case of the Preheater in Nickel Carbonyl Process

[+] Author and Article Information
Redhouane Henda1

School of Engineering, Laurentian University, Ramsey Lake Road, Sudbury, ON P3E 2C6, Canada

Daniel J. Falcioni

Noranda/Falconbridge Ltd., MTG Extractive Metallurgy, Falconbridge Technology Centre, Falconbridge, ON P0M 1S0, Canada

1

To whom correspondence should be addressed.

J. Appl. Mech 73(1), 47-53 (Apr 18, 2005) (7 pages) doi:10.1115/1.1991862 History: Received June 28, 2004; Revised April 18, 2005

Heat transfer in a two-dimensional moving packed bed consisting of pellets surrounded by a gaseous atmosphere is numerically investigated. The governing equations are formulated based on the volume averaging method. A two-equation model, representing the solid and gas phases separately, and a one-equation model, representing both the solid and gas phases, are considered. The models take the form of partial differential equations with a set of boundary conditions, some of which were determined experimentally, and design parameters in addition to the operating conditions. We examine and discuss the parameters in order to reduce temperature differences from pellet to pellet. The calculation results show that by adopting a constant temperature along the preheater outer wall and decreasing the velocity of the pellets in the preheater, the difference in temperature from pellet to pellet is reduced from 120°C to 55°C, and the thermal efficiency of the preheater is tremendously improved.

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Copyright © 2006 by American Society of Mechanical Engineers
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Figures

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Figure 8

Temperature profiles of the bed at the preheater outlet and at time t*=1. The corresponding conditions are indicated in the inset.

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Figure 1

Cross-sectional view of the industrial nickel carbonylation process (15)

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Figure 2

Schematic diagram of the moving packed bed in the preheater

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Figure 3

Space distribution of the solid phase dimensionless temperature in the preheater under standard process conditions and at time t*=1

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Figure 4

Transient dimensionless temperature profiles of the solid phase along the preheater at position r*=0.005 (a) and at the preheater outlet, x*=1 (b). The curves correspond to the dimensionless time range 0–1 with an increment of 0.1.

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Figure 5

Temperature difference between the fluid and solid phases along the preheater at position r*=0.005 and time t*=1. The figure in the inset is a “zoom-in” view of the region near the preheater inlet.

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Figure 6

Space distribution of the bed dimensionless temperature in the preheater under standard process conditions and at time t*=1

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Figure 7

Space distribution of the bed dimensionless temperature in the preheater at time t*=1 and corresponding to Twall=1 (a), c=0.1 (b), and to (a) and (b) combined (c).

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