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In spite of the effect of cycling on crystal size distribution(CSD)of potassium chloride in a pilot crystallizer, the average size can still be simulated by a steady-state approximate mathematical model.The CSD of this model in the main size range can be expressed as in MSMPR crystallizers.For fines and coarse crystals,the withdrawal of fines and the classification of coarse crystals are considered,respectively.For intermediate size,retention time of crystals is taken to be infinite for the analytical solution of the approximate model. When the settling zone and the elutriator of crystallizers are both ideal,the approximate model is reduced to a simplified model. The calculated values of linear growth rate G,dominant crystal size L_D,crystal size L_so corresponding to cumulative weight fraction of 50%,suspension density Mr,and productivity P/V all agree with the corres- ponding experimental data from a 0.52 m~3 pilot DTB crystallizer within 10% for both models.Design proce- dure of industrial crystallizers with elutriators is given.
In spite of the effect of cycling on crystal size distribution (CSD) of potassium chloride in a pilot crystallizer, the average size can still be simulated by a steady-state approximate mathematical model. The CSD of this model in the main size range can be expressed as in MSMPR crystallizers. For fines and coarse crystals, the withdrawal of fines and the classification of coarse crystals are considered, respectively. For intermediate size, retention time of crystals is taken to be infinite for the analytical solution of the approximate model. When the settling zone and the elutriator of crystallizers are both ideal, the approximate model is reduced to a simplified model. The calculated values of linear growth rate G, dominant crystal size L_D, crystal size L_so corresponding to cumulative weight fraction of 50%, suspension density Mr, and productivity P / V all agree with the corpus- ponding experimental data from a 0.52 m ~ 3 pilot DTB crystallizer within 10% for both models. Design proce dure of ind ustrial crystallizers with elutriators is given.