Reactors batch agitated

Agitated tank reactors Batch agitated reactor This is a batch stirred tank reactor. For liquid-solid systems, the liquid is agitated by a mechanical apparatus (impeller) and the reactor is of tank shape. For gas-solid systems, the gas is agitated and rapidly circulated through a fixed-bed of solids. This reactor is basically an experimental one used for adsorption, ion exchange, and catalysis studies. 

The reactor, an agitated tank, operates under a pressure of 1.5 kN/m2 (15 bar) and at 433 K (160°C). It is charged with a batch of 0.06 m3 of o-xylene and air introduced at the rate of 0.0015 m3/s (5.4 m3/h) measured at reactor conditions. The air is dispersed into small bubbles whose mean diameter is estimated from a photograph to be 0.8 mm, and from level sensors in the reactor, the volume of the dispersion produced is found to be 0.088 m3. Soon after the start of the reaction (before any appreciable conversion of the o-xylene) the gas leaving the reactor is analysed (after removal of condensibles) and found to consist of 0.045 mole fraction O2, 0.955 mole fraction N2. 

In connection with the engineering content of the book, a large number of reactors is analyzed two- and three-phase (slurry) agitated reactors (batch and continuous flow), two-and three-phase fixed beds (fixed beds, trickle beds, and packed bubble beds), three-phase (slurry) bubble columns, and two-phase fluidized beds. All these reactors are applicable to catalysis two-phase fixed and fluidized beds and agitated tank reactors concern adsorption and ion exchange as well. 

For example, Beltran and Alvarez (1996) successfully applied a semi-batch agitated cell for the determination of kL k,a, and the rate constants of synthetic dyes, which react very fast with molecular ozone (direct reaction, kD = 5 105 to 1 108 L mol-1 s l). In conventional stirred tank reactors operated in the semi-batch mode the mass transfer coefficient for ozone kLa(03) was determined from an instantaneous reaction of ozone and 4-nitrophenol (Beltran et al., 1992 a) as well as ozone and resorchinol (l,3-c//hydroxybenzene) or phloroglucinol... 

Neutralization of the sulfonic acid and building up with sodium sulfate and tetrasodium pyrophosphate (TSPP) is accomplished in two batch reactors (5 hr cycle) operated alternately. The sodium sulfate is pumped in solution with its transfer pump from the sodium sulfate system (which can be represented by a block). The TSPP is supplied as a solid and is fed by means of a Rcdler conveyor which discharges into a weigh hopper running on a track above the two reactors. Each reactor is agitated with a propeller and a turbine blade in a single shaft. 

Figure 17.9. Stirred tank reactors, batch and continuous, (a) With agitator and internal heat transfer surface, batch or continuous, (b) With pumparound mixing and external heat transfer surface, batch or continuous, (c) Three-stage continuous stirred tank reactor battery, (d) Three-stage continuous stirred tank battery in a single shell.

Vapours of ethylchloride are sent out of the reactor into expander 4, where solid particles deposit, and then condense in cooler 3. The condensate is returned to the synthesis through batch box 2. After the whole of ethylchloride has been supplied, the mixture in the reactor is agitated for 1 hour at 70-90 °C to complete the reaction. If in the absence of heat withdrawal the temperature begins to drop, it signifies the end of the reaction. If a rise in temperature is observed, it means that the reaction is not finished. In this case the process is conducted at 70-90 °C for a longer period, until heat release begins. 

Fig. 108. Production diagram of sodium /j-nitrophcnolatc (/ -NphNa) 1 -synthesis reactor 2 - agitator 3 - pump 4, 5 - batch boxes 6 - cooler 7 - collector...

No liquid flow-batch slurry reactor with agitation ... 

Batch, semi-batch and continuous emulsion polymerizations are usually carried out in stirred tank reactors, where agitation by a stirrer is necessary. The type of stirrer chosen and its stirring speed can often affect the rate of polymerization, the number of polymer particles and their size distribution (PSD), and the molecular weight of the polymer produced. However, the effect of stirring on emulsion polymerization has never been the main research parameter in research programs [241]. This is probably due to the conflicting results obtained so far by various researchers. 

N 2.5-6.0 low 0-50 Free drift Crushed seized limestone Batch reactor "vigorously agitated" 0.078 3.6 Barton and Vatanatham (38)... 

Also, polymerization reactions are carried out in a variety of reactors including agitated batch reactors, continuous stirred tank reactors (CSTR), multizone autoclaves, loop reactors, tubular reactors, fluidized bed reactors, and a combination of these reactors. 

Small-scale studies of the reaction indicate that diffusion resistance between particle surface and the gas is negligible. In a batch agitated reactor operated at the saihc temperature and gas composition, the following data were obtained ... 

A liquid-phase oxidation is carried out in aqueous solution in an agitated, sparged reactor. Batch tests show that the absorption rate decreases as the conversion increases, judging from the change in exit gas composition. The dissolved reactant and the product are nonvolatile, and the vapor pressure of the solution is about 80% that of water. The solution density is 60 Ib/ft. ... 

The typical reaction mechanism for tri-liquid PTC in a batch reactor under agitation is illustrated in the schematic diagram of Fig. 9. Three types of reaction scheme considering the partition of the catalyst in the different phases and the place where the inherent reaction occurred have been proposed [226,227]. For the substitution reaction of alkyl halide (RX) and aqueous reactant metal salt (MY) using quaternary ammonium salt (QX) as the catalyst, the different types of reaction are addressed as follows [226]. 

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