Batch reactor operation

Clearly, the oxidation reaction could not have been implemented in a pure batch operating reactor. Indeed, heat removal capacity would not have been sufficient (100—1200 kW m removed versus 20 x 10 kW m generated). As a consequence, a semibatch mode is necessarily required. Besides, Table 12.10 shows that the feeding times are much higher than the residence time of the Shimtec reactor (around 15 s). 

Equilibrium conversion (in %) in the high pressure batch operated reactor as a function of temperature and pressure. 

Example 4-1 Leyes and Othmer studied the formation of butyl acetate.in a batch-operated reactor at 100°C, with sulfuric acid as catalyst. The original feed contained 4.97 moles butanol/mole acetic acid, and the catalyst concentration was 0.032% by weight H2SO4. The following rate equation was found to correlate the data when an excess of butanol was used ... 

The reactor performance is defined as the amount of product A produced per unit time. In batch-operated reactors, depends on the entire reaction cycle The cycle consists of the reaction time required to reach a desired degree... 

Another important virtue of this scheme is that part of the alkaline polymerizate of the PO produced in reactor-polymerizer 2 (Fig. 1), of intermediate molecular weight, may be used further in batch operation setups, for the production of other grades of oligoethers. Reactors 2 and 5 are divided into sections by means of perforated partitions, so that each of them functions as an ideal mixing reactor while the number of sections is sufficient to ensure conditions in the liquid phase that yield the same molecular characteristics as those of the corresponding product from a batch operation reactor. 

Using a batch reactor, a constant concentration of sulfuric acid can be maintained by adding concentrated sulfuric acid as the reaction progresses, i.e., semi-batch operation. Good temperature control of such systems can be maintained, as we shall discuss later. 

Clearly, the time chart shown in Fig. 4.14 indicates that individual items of equipment have a poor utilization i.e., they are in use for only a small fraction of the batch cycle time. To improve the equipment utilization, overlap batches as shown in the time-event chart in Fig. 4.15. Here, more than one batch, at difierent processing stages, resides in the process at any given time. Clearly, it is not possible to recycle directly from the separators to the reactor, since the reactor is fed at a time different from that at which the separation is carried out. A storage tank is needed to hold the recycle material. This material is then used to provide part of the feed for the next batch. The final flowsheet for batch operation is shown in Fig. 4.16. Equipment utilization might be improved further by various methods which are considered in Chap. 8 when economic tradeoffs are discussed. 

Clearly, the potential hazard from runaway reactions is reduced by reducing the inventory of material in the reactor. Batch operation requires a larger inventory than the corresponding continuous reactor. Thus there may be a safety incentive to change from batch to continuous operation. Alternatively, the batch operation can be... 

The trend in the use of deep bed filters in water treatment is to eliminate conventional flocculators and sedimentation tanks, and to employ the filter as a flocculation reactor for direct filtration of low turbidity waters. The constraints of batch operation can be removed by using one of the available continuous filters which provide continuous backwashing of a portion of the medium. Such systems include moving bed filters, radial flow filters, or traveling backwash filters. Further development of continuous deep bed filters is likely. Besides clarification of Hquids, which is the most frequent use, deep bed filters can also be used to concentrate soflds into a much smaller volume of backwash, or even to wash the soflds by using a different Hquid for the backwash. Deep bed filtration has a much more limited use in the chemical industry than cake filtration (see Water, Industrial water treatment Water, Municipal WATERTREATiffiNT Water Water, pollution and Water, reuse). 

Applications One typical apphcation in heat transfer with batch operations is the heating of a reactor mix, maintaining temperature during a reaction period, and then cooling the products after the reaction is complete. This subsection is concerned with the heating and cooling of such systems in either unknown or specified periods. 

Because of the differences in primary and secondaiy metabolism, a reactor may have a dual-stage fed-batch system. In other words, fed-batch operation optimizes growth with little or no product formation. When sufficient biomass has accumulated, a different fed-batch protocol comes into play. 

Ethyl aluminum dichloride (EADC) is used in the rnanufacmre of certain catalysts for making LDPE. Occasionally, the batch operation involving the catalyst production results in an off-spec lot. This off-spec lot is washed from the reactor (impregantor) with water and hexane, and must be sent to a waste disposal facility. The facility treats this waste in a hydrolysis reaction (i.e., with water and mild agitation). If the reaction is exothermic, what are the potential air pollution and fire problems associated with the waste treatment ... 

A semi-batch reactor has the same disadvantages as the batch reactor. However, it has the advantages of good temperature control and the capability of minimizing unwanted side reactions by maintaining a low concentration of one of the reactants. Semi-batch reactors are also of value when parallel reactions of different orders occur, where it may be more profitable to use semi-batch rather than batch operations. In many applications semi-batch reactors involve a substantial increase in the volume of reaction mixture during a processing cycle (i.e., emulsion polymerization). 

Batch mixed reactor There are three principal modes of bioreactor operation (a) batch (b) fed batch (c) continuous. 

In this paper we present a meaningful analysis of the operation of a batch polymerization reactor in its final stages (i.e. high conversion levels) where MWD broadening is relatively unimportant. The ultimate objective is to minimize the residual monomer concentration as fast as possible, using the time-optimal problem formulation. Isothermal as well as nonisothermal policies are derived based on a mathematical model that also takes depropagation into account. The effect of initiator concentration, initiator half-life and activation energy on optimum temperature and time is studied. 

In case of exothermic reactions, the heat-exchange capacities of the reactor allow to rapidly evacuate the heat generated by the reaction and therefore to perform a transposition of a pure batch operating mode into a continuous one. The main point is the ability to avoid, as far as possible, an initial increase of the temperature as soon as the reactants are mixed. 

The transesterification reaction was carried out in a 50 mL stainless steel autoclave equipped with a magnetic stirrer. For each typical reaction, quaternary ammonium salt (2 mmol), propylene carbonate (25 mmol) and excess methanol (200 mmol) were charged into the reactor, and the CO2 was introduced at room temperature to a preset pressure. The reaction was started by stirring when the desired tranperature and pressure were attained The reachon was performed in a batch operation... 

Figure 1. Results of closed-loop operations (reactor A) (a) 9 batch without tuning, (b) 10 batch GA tuning...

Appropriate setting of two on-off valves (Fig. 1) allows the system to be operated either as a batch recycle reactor or as a continuous-flow steady-state recycle reactor. 

Figure 7. Effect of methane conversion on C2 selectivity for some of the best state-of-the-art OCM catalysts (A, based on ref 4), the simulated chromatographic reactor of Aris and coworkers (A, ref. 10) and the present work. ( ) Ag electrocatalyst, single pass (O) Ag electrocatalyst with recycle and trapping (0) Sr/LagOg catalyst, single pass ( ) Sr/La20g catalyst with recycle and trapping. Open symbols, batch operation filled symbols, continuous-flow steady-state operation.

A simplified mathematical model was developed for the novel OCM reactor. One version of the model, presented here, describes batch operation. A second version addressing continuous flow operation will appear elsewhere [16]. 

Methane can be oxidatively coupled to ethylene with very high yield using the novel gas recycle electrocatalytic or catalytic reactor separator. The ethylene yield is up to 85% for batch operation and up to 50% for continuous flow operation. These promising results, which stem from the novel reactor design and from the adsorptive properties of the molecular sieve material, can be rationalized in terms of a simple macroscopic kinetic model. Such simplified models may be useful for scale up purposes. For practical applications it would be desirable to reduce the recycle ratio p to lower values (e.g. 5-8). This requires a single-pass C2 yield of the order of 15-20%. The Sr-doped La203... 

For a Michael addition, however, the same isomeric ratio (99% trans 1% cis) was observed for micro-reactor and batch operations [151]. 

For example, the hydrogenation of methyl (Z)-a-acetamidocinnamate gives a chiral product when conducted in the presence of a chiral diphosphine catalyst. The enantiomeric excess data for micro-reactor and batch operation are in line when performed imder similar conditions [169]. A very high reproducibility of determining data on enantiomeric excess was reported [170]. In addition, the ee distribution was quite narrow 90% of aU ee data were within 40-48% [170]. 

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