Height of bed

N Number of velocity heads lost through unit height of bed m-1 L-1... 

In equation 6.67, Q may be obtained from the change in temperature of the gas stream, and a, the area for transfer per unit height of bed, from measurements of the surface of solids in the bed. In this case, the integration may be carried out graphically, because the relation between AT and z was obtained from the readings of the thermocouple. The temperature recorded by the thermocouple was assumed to be the gas temperature, and,... 

Absolute density. Particle- Type of Vessel Height of Bed Flow range. ... 

The static bed height in the fluidized bed is usually expressed in terms of the ratio of the static height of bed materials (//) to the column diameter (D). A bed height... 

A set of morphologic states characterized by state descriptors (i.e., mean bed slope, and mean height of bed morphology), and their spatial probability distributions. 

The schematic for this system, where the draft tube is operated as a fluidized bed rather than a dilute phase pneumatic transport tube, is shown in Fig. 5. A mathematical model for the system was developed by LaNauze (1976). The driving force for solids circulation in this case was found to be the density difference between draft tube and downcomer. The solids circulation rate was also found to be affected only by the distance between the distributor and the draft tube and not by the draft tube length or height of bed above it. Because of the lower velocity in the draft tube, the... 

The optimum particle size depends on the gas flow and the specific bed characteristics in question. As the size of catalyst particles affects the reactor bed diameter, the particle size of catalysts should be chosen based on the type and diameter of reactor, height of beds and specific plant conditions. 

H]) height of bed corresponding to the dense phase only, m bed height at minimtun bubbling conditions, m bed height at minimtun fluidization conditions, m K proportionality constant... 

Figure 5.17 shows the corresponding pressure drops per unit height of bed. These are higher than those calculated from standard correlations. 

The ability to attain smooth fluidisation over reasonably broad bed expanses depends on a proper balance of such parameters as particle size, particle size distribution, particle shape, flow character of the powder, gas velocity, humidity, ratio of height of bed to diameter, and pore size and pore volume of distributor plate. 

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