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230  Dust Explosions in the Process Industries


             3.6.3
             ENTRAINMENT OF  PARTICLES BY AN UPWARD AIRFLOW
            THROUGH A  PARTICLE BED

            Entrainment of particles of equal shape in a fluidized bed configuration, illustrated in
            Figure 3.23, was studied by Schofield, Sutton, and Waters (1979).


              I        ‘  -.         - ..  1.
                                 -.
              1;:  :I  .  ..,  .. .’.I.
                                   .-
             .I.‘  .  .   ‘  ZONE  A   .  .+.’I.
                       .  .      .   . .  *  .-
                                         . I .
                             ..
                     .  .
              -1  ..
             _-_---___
                                ’
                 *..e  .    * . . .** .  -1..
             .*I.#  :.  ,-             -. .
                .  . . ..  ZONE E.**    e  I;
                       .-  0  .  .   f   ..




              1                            I      bed (From Schofield et a/., 1979).
                                                  Figure 3.23  The emission of dust from a fluidized


               Let v, be the minimum local air velocity inside zone C needed to lift a particle of aero-
             dynamic cross section a, from zone C into zone B, and v,  be the average vertical airveloc-
             ity in zones B and A corresponding to v, in zone C. Often, v,  is denoted the “superficial”
             gas velocity through a fluidized bed. Because the effectivecross section for vertical air-
             flow in zone C is smaller than in zones A and B, v,  < y,.  Therefore, the largest particles
             injected from zone C to zone B drop back into zone C. Only particles of aerodynamic
             cross sections smaller than a maximum value a,  are lifted further into zone A. At a
             given v,,  all the particles in zone C of smaller aerodynamic cross section than a, even-
             tually are extracted from zone C and pass through zone B into zone A. Therefore, the
             concentration of these particles in zone C can be regarded as only approximately con-
             stant during the initial phase of  the fluidization process. This was accounted for in the
             investigation by Schofield et al. (1979), who used a fluidized bed of 46 cm2cross sec-
             tion in their experiments. All experimental data were acquired during the initial flu-
             idization phase. Grade emission curves, illustrated in Figure 3.24, were determined for
             a chalk powder exposed to various values of v,.
               The grade emissioncurveexpressesthe mass per unit time at which particles smallerthan
             a given size are emitted from the bed under a given set of experimental conditions.For exam-
             ple, with reference to Figure 3.24 and 0.205 m/s airvelocity, particles smaller than 10 pm
             are emitted at a rate of 20 mg/min, whereas particles smaller than 2 pm are emitted at
             4.5 mg/min. This means that particles between 10 and 2 pm are emitted at 15.5 mg/min.
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