This table includes three geometric scaleup factors. Factors for other forms of scaleup for incompressible fluids are given in Table 10.2. When scaling in parallel, the number of tubes scales directly with the inventory scaleup factor, S. This advantage is especially useful in polypropylene processes where the last reactor adds ethylene for impact modification. The usual case is for two Ī major advantage of using tanks in series is the ability to have a different reaction environment in the various tanks. The series arrangement leads to higher conversion and thus eases the burden of downstream recovery and recycling. One advantage of using tanks in series is the improvement in residence time distribution from the exponential distribution of a single stirred tank toward that of piston (plug) flow. Modern fluidized-bed processes for polypropylene use two beds in series. Some polypropylene processes use two or three loop and stirred-tank reactors in series. Some polystyrene processes use five stirred-tank and stirred- tube reactors in series.
Another way is to add a stirred tank in parallel, but better results and a more flexible process are usually achieved by adding a stirred tank in series. One way to double the output of a stirred tank process is to increase each linear dimension by 2 / = 1.26, but this may lead to heat transfer or mixing limitations. For the same LIG ratio, the relative crystallization times of k stages and one stage to reach the peaks are given by Eq. For two such the cumulative distribution is represented by Īs in the operation of chemical reactors, multistaging requires shorter residence time for the same performance.
Nyvlt (1971) also develops equations for multistage crystalhzers in which nuclei form at the same rate in all stages. Wilh generation of nuclei in die first stage only, the Equations were developed by Nyvlt (1971) for two main cases.
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