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Minimum Fluidizing Velocities for Various Bed Packings

Learn about the minimum fluidizing velocities for different bed packings. This study covers theoretical and experimental approaches, results, and conclusions. Discover the challenges and results of fluidization research.

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Minimum Fluidizing Velocities for Various Bed Packings

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  1. Minimum Fluidizing Velocities for Various Bed Packings By Andrew Maycock

  2. Introduction to Fluidization • Fluid flowed through bottom of a fixed bed • Fluidization is the balance of gravity, drag and buoyant forces • Suspended particles have larger effective surface area than a packed fixed bed • The smallest velocity at which fluidization occurs is the minimum fluidization velocity

  3. Fluidization Apparatus Figure 1: Example of fluidization bed

  4. Overview • Theoretical Approach • Experimental Approach • Results • Method Summaries • Conclusions • Q&A

  5. Theoretical Approach • Bernoulli’s Equation • Correlations for friction loss terms through porous media

  6. Ergun Equation • Sphericity term included • Composed of known or obtainable parameters

  7. Minimum Fluidizing Velocity • Ergun Equation solved simultaneously with force balance. • May assume that flow is laminar (NRe < 20) (Equation reduces to laminar friction term)

  8. Experimental Approach Figure 2: Example of fluidization bed

  9. Determining MFV • Change occurs in slope of pressure drop plot Figure 3: Plot of pressure drop vs. Fluid Velocity

  10. Particle Properties • Graduated cylinder for bed density • Displaced volume for particle density • Microscopic photos for sphericity

  11. Experimental Procedure • Glass Beads and Pulverized Coal • Increase mass flowrate • Measure pressure drop across bed • Change temperature and repeat • Determine fluid properties using correlations and equations of state

  12. Experimental Problems • Poor Distribution • Faulty or imprecise pressure gauges • Difficulty in determining when fluidization has been reached

  13. Results

  14. Pulverized Coal Results Figure 3: Microscopic photo of pulverized coal

  15. Pulverized Coal Results (cont.) Figure 4: Pressure drop data and Ergun Equation for pulverized coal at 26.2 °C

  16. Pulverized Coal Results (cont.) Figure 5: Pressure drop data and Ergun Equation for pulverized coal at 32.8 °C

  17. Pulverized Coal Results (cont.) Figure 6: Pressure drop data and Ergun Equation for pulverized coal at 39.9 °C

  18. Pulverized Coal Results (cont.) Example of results for pulverized coal

  19. Glass Bead Results Figure 7: Microscopic photo of glass beads

  20. Glass Bead Results (cont.) Figure 8: Pressure drop data and Ergun Equation for glass beads at 30.0 °C

  21. Glass Bead Results (cont.) Figure 9: Pressure drop data and Ergun Equation for glass beads at 37.8 °C

  22. Glass Bead Results (cont.) Figure 10: Pressure drop data and Ergun Equation for glass beads at 42.1 °C

  23. Glass Bead Results (cont.) Example of results for glass beads

  24. The Laminar Assumption

  25. The Laminar Assumption (cont.) • Reported to be accurate for Particle Reynolds Numbers under 20 • More accurate as Reynolds Numbers get smaller • Typical values within 15-30% of Ergun Equation • Has no consistent relation to experimental value

  26. Experimental Summary • Experimental determination is accurate and necessary • Difficult to determining exact value for minimum fluidizing velocity • Error in minimum fluidizing velocity measurement based on test interval

  27. Correlation Summary • Provide a good estimate for actual fluidizing velocity. • Require difficult estimation of bed height and void fraction for operation above minimum fluidizing velocity. • Ergun Equation can show unrealistic results, as in this case. • Decent estimation requires accurate particle property values (void fraction and particle density are difficult to determine due to adsorption).

  28. Conclusions • Correlations are useful, but not substitute for actual experimentation • Experimentation necessary because of inaccurate and imprecise instrumentation • Correlations are useful for industrial processes which are usually operated at two to three times the minimum fluidizing velocity

  29. References • de Nevers, Noel, Air Pollution Control Engineering, 2nd ed. Mc-Graw Hill, New York (2005). • de Nevers, Noel, Fluid Mechanics for Chemical Engineers, 3rd ed. Mc-Graw Hill, New York (2005). • Seader, J.D. and Henley, Ernest J., Separation Process Principles, 2nd ed.Wiley, Danver, Massachusetts (2006). • Wikipedia, Sphericity, http://en.wikipedia.org/wiki/Sphericity

  30. Questions • 5 Minute Question Period

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