Fig. 23 Baffle plate above surface. (From Ref. 29.) portant to avoid air incorporation or foaming), the baffle plate can be lowered to pre-vent splashing. This allows the mixer to be emulsifying at highest speed and, hence, highest shearing rates while avoiding aeration. All mixers or mixing systems must provide flow to all areas of the process ves-sel if they are to be deemed successful. In the case of these axial-flow rotor/stator mixers, the flow emanates from the mixing head and flows in a single direction. In order for the flow to reach every area of the vessel, it must deflect off the baffle plate and then the sidewall. If the mixer cannot produce enough flow to reach the sidewall, then a dead spot exists. The amount of flow required and the amount of flow produced by a given size mixer depends on the viscosity and the design of the specific mixer. The manufacturer should know the pumping capabilities of their mixers at different viscosities in order to select equipment for different size mixing vessels. Table 4 shows the abil-ity of a typical axial-flow rotor/stator mixer. The batch size that can be handled on a macroscale basis can be determined from Table 4 for the axial-flow rotor/stator mixer if the diameter of the process vessel and the diameter of the rotor are known. This is a trial-and-error problem. By choosing a batch size, vessel diameters can be obtained by use of standard-size vessels. If a fea-sible mixer can be installed in a standard-size vessel, the total system capital cost can probably be lowered. The rotor diameters that are available for trial-and-error solution are usually set by the manufacturer. That is, various sizes are available but not an in-finite variety. As an example, take a 1000 gal. process tank with a 72 in. diameter. If a6.5 in. diameter rotor unit is used, a viscosity of up to about 9000 centipoise can be pumped

DOI link for Fig. 23 Baffle plate above surface. (From Ref. 29.) portant to avoid air incorporation or foaming), the baffle plate can be lowered to pre-vent splashing. This allows the mixer to be emulsifying at highest speed and, hence, highest shearing rates while avoiding aeration. All mixers or mixing systems must provide flow to all areas of the process ves-sel if they are to be deemed successful. In the case of these axial-flow rotor/stator mixers, the flow emanates from the mixing head and flows in a single direction. In order for the flow to reach every area of the vessel, it must deflect off the baffle plate and then the sidewall. If the mixer cannot produce enough flow to reach the sidewall, then a dead spot exists. The amount of flow required and the amount of flow produced by a given size mixer depends on the viscosity and the design of the specific mixer. The manufacturer should know the pumping capabilities of their mixers at different viscosities in order to select equipment for different size mixing vessels. Table 4 shows the abil-ity of a typical axial-flow rotor/stator mixer. The batch size that can be handled on a macroscale basis can be determined from Table 4 for the axial-flow rotor/stator mixer if the diameter of the process vessel and the diameter of the rotor are known. This is a trial-and-error problem. By choosing a batch size, vessel diameters can be obtained by use of standard-size vessels. If a fea-sible mixer can be installed in a standard-size vessel, the total system capital cost can probably be lowered. The rotor diameters that are available for trial-and-error solution are usually set by the manufacturer. That is, various sizes are available but not an in-finite variety. As an example, take a 1000 gal. process tank with a 72 in. diameter. If a6.5 in. diameter rotor unit is used, a viscosity of up to about 9000 centipoise can be pumped

Fig. 23 Baffle plate above surface. (From Ref. 29.) portant to avoid air incorporation or foaming), the baffle plate can be lowered to pre-vent splashing. This allows the mixer to be emulsifying at highest speed and, hence, highest shearing rates while avoiding aeration. All mixers or mixing systems must provide flow to all areas of the process ves-sel if they are to be deemed successful. In the case of these axial-flow rotor/stator mixers, the flow emanates from the mixing head and flows in a single direction. In order for the flow to reach every area of the vessel, it must deflect off the baffle plate and then the sidewall. If the mixer cannot produce enough flow to reach the sidewall, then a dead spot exists. The amount of flow required and the amount of flow produced by a given size mixer depends on the viscosity and the design of the specific mixer. The manufacturer should know the pumping capabilities of their mixers at different viscosities in order to select equipment for different size mixing vessels. Table 4 shows the abil-ity of a typical axial-flow rotor/stator mixer. The batch size that can be handled on a macroscale basis can be determined from Table 4 for the axial-flow rotor/stator mixer if the diameter of the process vessel and the diameter of the rotor are known. This is a trial-and-error problem. By choosing a batch size, vessel diameters can be obtained by use of standard-size vessels. If a fea-sible mixer can be installed in a standard-size vessel, the total system capital cost can probably be lowered. The rotor diameters that are available for trial-and-error solution are usually set by the manufacturer. That is, various sizes are available but not an in-finite variety. As an example, take a 1000 gal. process tank with a 72 in. diameter. If a6.5 in. diameter rotor unit is used, a viscosity of up to about 9000 centipoise can be pumped