Batch reactor high pressure

For high-pressure operation, safety considerations are extremely important and care must be taken to ensure proper mechanical design. Closures must be designed to withstand the same maximum pressure as the rest of the autoclave. Various authors have treated the problems involved in designing medium- and high-pressure batch reactors (2-4). 

As mentioned earlier in section 2.2, a two-step mechanism via intermediate formation of methanol has been proposed by Adebajo et al, [21-23, 26, 36] for the oxidative mcthylation of benzene with methane over acidic zeolites in a high-pressure batch reactor. In view of this mechanism, a preliminary investigation has been carried out by these workers [24] on the reaction of toluene with methane over acidic ZSM-5 catalysts in a batch reactor containing residual air to determine the actual contribution of direct mcthylation (via intermediate methanol formation) to the observed reaction products. The reactions were carried out at 400 C and 6.9 MPa pressure. The major reaction products obtained by these wwkers were benzene and xylenes. Smaller amounts of ethylbenzene, trimethylbenzene and other higher aromatics were also produced. Over acidic catalysis, the conversion of toluene can, in principle occur through two different reaction pathways mcthylation by methane via methanol (as in the case of benzene mcthylation) and disproportionation, as shown in equations (4) and (S) below ... 

Several MOFs as UIO-66, UIO-ee-NH, Mg-MOF-74, MIL-101, CuBTC, ZIF-8, IRMOF-3, and MOF-5 with different acid-base properties were tested as catalysts for the synthesis of styrene carbonate (SC) from styrene oxide (SO) with CO using a high-pressure batch reactor [116]. 

T2 Laboratories manufactured a fuel additive, methylcyclopeniadienyl manganese iricarbonyl (MCMT), in a 2.450-gallon, high-pressure batch reactor utilizing a three-step batch process. 

Glucose hydrogenation has been studied in a well-stirred, high-pressure batch reactor on promoted Raney-Ni catalysts [13]. Mo, Cr, Sn, and Fe were reported to... 

Figure 9.2-1. Design of experimental batch-stirred-tank apparatus for synthesis under high pressure 1, reactor 2, separator P, high pressure pump PI, pressure indicator [17].

Economic evaluations were made for the enzyme-catalyzed production of oleyl oleate in a high-pressure batch-stirred-tank reactor (HP BSTR) and in a high-pressure continuously... 

Reaction performance. Supercritical carbon dioxide was used as a reaction media for the enzymatic synthesis of oleyl oleate directly from oleic acid and oleyl alcohol. Reaction was catalyzed by immobilized lipase from Rhizomucor miehei-Ltpozyme IM. Reactions were carried out in the high pressure batch and continuous reactor. 

High pressure batch stirred tank reactor. Substrates (equimolar solution of oleic acid and oleyl alcohol) were filled into thermostated autoclave and mixed. Enzyme preparation was added and finally CO2 was pumped with a high pressure pump up to desired pressure. Reactor volume was 0.5 L (Pmax = 450 bar, Tmax = 200°C) (Figure 1). 

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

Figure 2.1-9 Scheme of a single batch high pressure view reactor. 

Emulsion homopolymerization or copolymerization of MMA is usually carried out in a pressurized batch reactor with a water-soluble initiator and surfactant. The polymerization temperature may be varied from 85 C to 95 C to achieve high conversion. Bacterial attack, common in acrylic polymer... 

The complex batch reactor is a specialized pressure vessel with excellent heat transfer and gas Hquid contacting capabiUty. These reactors are becoming more common in aLkylphenol production, mainly due to their high efficiency and flexibiUty of operation. Figure 2 shows one arrangement for a complex batch reactor. Complex batch reactors produce the more difficult to make alkylphenols they also produce some conventional alkylphenols through improved processes. 

The same four operating steps are used with the complex batch reactor as with the simple batch reactor. The powerhil capabiUties of the complex batch reactor offset their relatively high capital cost. These reactors can operate at phenol to alkene mole ratios from 0.3 to 1 and up. This abiUty is achieved by designing for positive pressure operation, typically 200 to 2000 kPa (30 to 300 psig), and for the use of highly selective catalysts. Because these reactors can operate at low phenol to alkene mole ratios, they are ideal for production of di- and trialkylphenols. 

Pure zirconium tetrachloride is obtained by the fractional distillation of the anhydrous tetrachlorides in a high pressure system (58). Commercial operation of the fractional distillation process in a batch mode was proposed by Ishizuka Research Institute (59). The mixed tetrachlorides are heated above 437°C, the triple point of zirconium tetrachloride. AH of the hafnium tetrachloride and some of the zirconium tetrachloride are distiUed, leaving pure zirconium tetrachloride. The innovative aspect of this operation is the use of a double-sheU reactor. The autogenous pressure of 3—4.5 MPa (30—45 atm) inside the heated reactor is balanced by the nitrogen pressure contained in the cold outer reactor (60). However, previous evaluation in the former USSR of the binary distiUation process (61) has cast doubt on the feasibHity of also producing zirconium-free hafnium tetrachloride by this method because of the limited range of operating temperature imposed by the smaH difference in temperature between the triple point, 433°C, and critical temperature, 453°C, a hafnium tetrachloride. 

Another common situation is batch hydrogenation, in which pure hydrogen is introduced to a relatively high pressure reactor and a decision must be made to recycle the unabsorbed gas stream from the top of the reactor or use a vortexing mode for an upper impeller to incorporate the gas from the surface. 

Biocatalysts in nature tend to be optimized to perform best in aqueous environments, at neutral pH, temperatures below 40 °C, and at low osmotic pressure. These conditions are sometimes in conflict with the need of the chemist or process engineer to optimize a reaction with respect to space-time yield or high product concentration in order to facilitate downstream processing. Furthermore, enzymes and whole cells are often inhibited by products or substrates. This might be overcome by the use of continuously operated stirred tank reactors, fed-batch reactors, or reactors with in situ product removal [14, 15]. The addition of organic solvents to increase the solubility of substrates and/or products is a common practice [16]. 

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