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On the Mac, use the Displays system preference to change your monitor s bit depth. In Windows XP, use the Settings pane of the Display control panel. In Windows Vista, use the Display Settings control panel (which you typically access from the Personalization control panel).

There is no simple way to describe the distribution of solids in a stirred vessel The techniques described here either give accurate quantitative data on local concentrations of solids (conductivity probe, optical probe, sampling for external analysis, or process tomography), or provide general observations and semiquantitative information (eg, cloud height) on the distribution of solids (visual observation, process tomography) If several local measurements are made using the conductivity, optical, or sampling techniques described below, the relative standard deviation of the data can be used to give a single measure of how well the solids are distributed The reader is cautioned that this quantity is extremely sensitive to the number and location of the data points used and is of little use without reference to visual observations and a full record of the local data measurement locations used to calculate it.

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The tubular reactor with static mixers was chosen for the documented capability of static mixers to accomplish the following important functions for fast multiple reactions in turbulent ow: (1) homogeneity down to the molecular level can be achieved in a few tube diameters; (2) very short mixing time and narrow residence time distributions are required; and (3) high rates of energy dissipation are achievable (average energy dissipation rates can be calculated from pressure drop and local rates can be estimated) The cooling capability of static mixers under conditions of extremely rapid heat generation is very low, leading to solvent evaporation in the mixing elements This two-phase ow reduced the residence time further The tubular reactor with static mixing elements discharged into a stirred tank, where evaporation and condensation removed the heat Yields in the tubular reactor were 15 to 25% better than in the stirred tank, depending on ow rate.

Two types of probe have commonly been used: conductivity and optical Both types of probes and the associated instrumentation are commercially available, but care should be taken to ensure that the probe and instrumentation are suitable for a particular application The dimensions of the measuring volume should be at least an order of magnitude greater than the dimensions of the solid particles, and the probe should allow free ow through the measuring volume If these criteria cannot be met, inaccurate measurements will result, and a custom-built probe may have to be used Attempts to close a solids mass balance using these approaches generally fail unless the solids are very well distributed throughout the vessel It is very dif cult to measure accurately the quantity of any unsuspended solids on the vessel base This problem is most acute if visual observations are not possible.

This reactor con guration was also superior to the wiped lm evaporator, possibly for two reasons: (1) higher rates of turbulence energy dissipation achieved more rapid micromixing, and (2) superior mixing at the entrance to the static mixers compared to the entrance of the wiped- lm evaporator, where some backmixing took place The possible signi cance of backmixing in fast multiple reactors is underscored by this example and is also discussed by Bourne et al (1981) and by Bourne and Garcia-Rosas (1984) If the heat rise in the tubular reactor (unspeci ed) could not have been tolerated, the wiped- lm evaporator with more effective convective heat removal (since more surface area to volume is achieved) would have been required Resolution: A static mixer reactor was superior to a wiped- lm evaporator in yield Heat removal was accomplished in a subsequent ash vessel.

Message: This example is illustrative of the necessity to meet multiple criteria, including liquid liquid dispersion, short contact time, minimum backmixing, and high heat transfer rates, in a single reactor con guration The heat transfer rate, however, was not achievable in an on-line mixer that could achieve the mixing criteria because of the extremely short contact time Use of ash evaporative cooling at the reactor discharge is an excellent example of effective process integration..

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