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A: A fully baf ed 200 L vessel with a 22 cm Rushton turbine Addition points are on the surface and into the impeller discharge stream (Table 13-6) These results continue to indicate mixing sensitivity, indicating that extreme caution must be taken on scale-up to manufacturing The effect of addition time is not as expected for a classic consecutive-competitive reaction system, suggesting that the reaction pathway contains a step that requires maintaining short addition time on scale-up Note: This kind of unexplained difference in result is not uncommon, and in many cases, time does not permit nding the exact cause as long as the negative effect can be overcome by effective design Q: What vessel and mixing system would you specify for manufacturing that would achieve laboratory results A: The production requirements for this step of a multistep process require a 10 m3 (10 000 L) stirred tank.





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The sensitivity to mixing experienced in the experiments above indicates that scale-up to this size vessel may not be feasible to obtain expected yield The complication of the unexpected sensitivity to addition time further indicates that an alternative design is indicated Alternatives to be considered: Multiple injection points in the tank Rapid recycle loop on a standard reactor for addition into the high-shear zone In-line mixer device in semicontinuous operation In-line premixing of the reactants with a static mixer was selected since this method of operation was compatible with the overall process design, and the mixing intensity required could be expected at the size and throughput required Solution: A static mixer was developed successfully for production scale operation, as shown schematically in Figure 13-10 The mixer chosen was a static mixer with an L/D ratio of 4 The nominal residence time of the combined twoliquid-phase stream was 1 s.

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The Reynolds number in the mixer was 2000 based on empty tube diameter The reactant mole ratio was 095 to 10 mol B/A Results for the static mixer in both laboratory scale 0008 m (08 cm) and plant scale 00254 m (254 cm) operation were excellent No change in selectivity or product distribution occurred over this scale-up When there are compelling reasons to use a semibatch reactor instead of a semicontinuous system, the reactor.

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