In spite of the effect of cycling on crystal size distribution(CSD) of potassium chloride in a pilot plant crystallizer

the average size can still be simulated by a steady-state mathematical model. According to this model

the CSD in the main size range for industrial crystallizers may be expressed as an exponential function of the population density n with respect to crystal size L

as for mixed-suspension-mixed-product-removal (MSMPR) crystallizers. For fine and coarse crystals

the withdrawal of fines and the classification of coarse crystals

respectively

should be taken into account as in the case of the R-Z model. For intermediate crystals

which can settle behind the baffles and can not be drawn off effectively from the elutriator

their retention time is taken to be infinite for simplification. The resulting mathematical model is expressed by Eqs. ( 2 )-( 5 ) and illustrated in Fig. 2. This model is a generalized form of all previous models for crystallizers. The calculated CSD in the main-size range fits well data from a 520-liter pilot-plant crystallizer. The calculated values for crystal growth rate G

dominant crystal size LD

median crystal size L50

suspension density MT

and production rate P/V

all agree

within 10%

with the corresponding experimental data. However

the MT equation

Eq. (10)

is rather complicated

so a. simplified model

in which LF = 0 and Z = ∞

is derived

and a simplified MT equation

Eq. (11)

is used for crystallizer design. The design Procedure for industrial crystallizers with elutriators is also given.