Atch reactor

CSTR is used when intense agitation is required. Figure l-7(a) showed a cutaway view of a Pfaudler CSTR atch reactor. Table 1-1 gives the typical sizes (along with that of the comparable size of a familiar object) and costs for batch and CSTR reactors. All reactors are glass lined and the prices include heating/cooling jacket, motor, mixer, and baffles. The reactors can be operated at temperatures between 20 and 4. )0 F and at pressures up to 100 psi. 

Procedure Cholinesterase activity in analyzed tissue or the matrix (biotest with immobilized AChE) is determined in the incubation media [consisting of substrate ATCh - 34 mmol maleate buffer 0.1 M, pH = 6.0- 6.5 ml sodium citrate 0.1 M - 0.5 ml CuS045H20 0.03M -1.0 ml distilled H20 (or inhibitor in variant with toxin analyzed) -1.0 ml potassium ferricyanide 0.005 M -1 ml.] Volume of incubation media in one test - 400 mcl. As a blank (control sample), a treatment of the exposure without the substrate is used. If inhibitory effects of allelochemical (or any toxin) are analyzed, before the substrate addition the sample was preliminary exposed to allelochemical inhibitor. Two methods for the AChE-biotests may be recommended (i) in microcells ( stationary conditions ) and (ii) in flowing columns-reactors ( dynamic conditions ). 

If the enzyme charged to a batch reactor is pristine, some time will be required before equilibrium is reached. This time is usually short compared with the batch reaction time and can be ignored. Furthermore, xo 5 Eq is usually true so that the depletion of substrate to establish the equilibrium is negligible. This means that Michaelis-Menten kinetics can be applied throughout the reaction cycle, and that the kinetic behavior of a batch reactor will be similar to that of a packed-bed PFR, as illustrated in Example 12.4. Simply replace t with tf,atch to obtain the approximate result for a batch reactor. 

Figure 6-18 Straight-through transport reactor. [From V. Weekman,/4/CA J. 20, 833, (1974) with permission of the AtChE. Copyright 1974 AICHE. AU rights reserved.]...

In general the conversion of reactant is not a very useful term for seihib atch operatidhbecause when reactant is present initially in the reactor and is added and deleted in feed and exit streams, there may be ambiguity about the total amount upon which to define x. Instead we shall formulate Eq. (3-1) in terms of the mass fraction w of reactant. If Fq is the total mass feed rate and Fj, is the withdrawal rate, the mass balance for the reactant is... 

Production rate of L-aspartic acid from a 10,000 gallon reactor is 1020 kgT)atch using a batch time of 35 hr. 

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