Reactors Summary table

Click the Reactions tab, then select the Results page. The conversion appears in the Reactor Results Summary table. 

Other types Other reactors are covered in applications chapters, notably nuclear reactors (Chapter 10) and the gas turbine reactor and turbo cracker (Chapter 9). Table 5.5 summarises a selection of intensified reactors, merits, limitations and potential uses. Table 5.5 Summary table on various intensified reactors. ... 

Chapter 4 provides summary tables of reactor concepts and designs addressed in this report, including ... 

Dead Seas Periclase Ltd., on the Dead Sea in Israel, uses yet another process to produce magnesium oxide. A concentrated magnesium chloride brine processed from the Dead Sea is sprayed into a reactor at about 1700°C (127,128). The brine is thermally decomposed into magnesium oxide and hydrochloric acid. To further process the magnesia, the product is slaked to form magnesium hydroxide which is then washed, filtered, and calcined under controlled conditions to produce a variety of MgO reactivity grades. A summary of MgO purities, for the various processes is given in Table 20. 

The reactor yield is then determined by performing a component balance. The amount of C5+ in the gasoline boiling range is calculated by subtracting the C4 and lighter components from the total gas plant products. Example 5-4 shows the step-by-step calculation of the component yields. The summary of the results, normalized but unadjusted for the cut points is shown in Table 5-4. 

A summary of the nine batch reactor emulsion polymerizations and fifteen tubular reactor emulsion polymerizations are presented in Tables III IV. Also, many tubular reactor pressure drop measurements were performed at different Reynolds numbers using distilled water to determined the laminar-turbulent transitional flow regime. 

Continuous Polymerizations As previously mentioned, fifteen continuous polymerizations in the tubular reactor were performed at different flow rates (i.e. (Nj g) ) with twelve runs using identical formulations and three runs having different emulsifier and initiator concentrations. A summary of the experimental runs is presented in Table IV and the styrene conversion vs reaction time data are presented graphically in Figures 7 to 9. It is important to note that the measurements of pressure and temperature profiles, flow rate and the latex properties indicated that steady state operation was reached after a period corresponding to twice the residence time in the tubular reactor. This agrees with Ghosh s results ). 

Table 1 Summary of primary MSO reactor test conditions...

Commercially available processes for resid HCK deal with catalyst life cycle issues by the use of different catalyst/reactor/configuration arrangements. In Ref. [142], Morel et al. discuss the performance and features of these arrangements. A summary of conditions for each reaction system is collected in Table 11. 

Table 11 Summary of results for ideal reactor models0,4 ...

The choice of appropriate reaction conditions is crucial for optimized performance in alkylation. The most important parameters are the reaction temperature, the feed alkane/alkene ratio, the alkene space velocity, the alkene feed composition, and the reactor design. Changing these parameters will induce similar effects for any alkylation catalyst, but the sensitivity to changes varies from catalyst to catalyst. Table II is a summary of the most important parameters employed in industrial operations for different acids. The values given for zeolites represent best estimates of data available from laboratory and pilot-scale experiments. 

Table 10.4-1. Summary of trends in the deposition rate and non-uniformity responses to increases in each of the geometric parameters in the reactor.

Reductive Carbonylation of Methanol. The reductive carbonylation of methanol (solvent free) was studied at variable I/Co, PPh,/I, temperature, pressure, synthesis gas ratio and methanol conversion (gas uptake) in the batch reactor, A summary of the results is given in Table I. In general, the acetaldehyde rate and selectivity increase with increasing I/Co. The PPh /I ratio has little effect except in run //7 where the rate is drastically reduced at I/Co =3.5 and PPh /I r 2. A good set of conditions is I/Co =3 5 and PPh /I = 1,T where the acetaldehyde rate and selectivity is 7.6 M/nr and 765 at 170 °C and 5000 psig. The effect of methanol conversion at these conditions is obtained by compearing runs 13, 1, 14, and 15. The gas uptake was varied from 14000 to 4000 psi, which corresponds to observed methanol conversions of 68% to 38 te. 

Table 7.9 Monthly statistical analysis and concrete mix design summary sheet Area Reactor building...

TABLE 1 Summary of Estimated Costs in Dollars/Ton (0.90718 metric ton) for Various Feed Rates and Influent Concentrations for Gas-Phase Corona Reactor Treatment of Volatile Organic Compounds... 

Numerous modeling studies of CVD reactors have been made and are summarized in recent review papers (I, 212). Table 3 in reference 212 lists major examples of CVD models up to mid-1986. Therefore, rather than giving an exhaustive list of previous work, Table V presents a summary of the major modeling approaches and forms the basis for the ensuing discussion, which is most appropriately handled in terms of two groups (1) hot-wall LPCVD systems and (2) cold-wall, near-atmospheric-pressure reactors. In LPCVD reactors, diffusion and surface reaction effects dominate, whereas in cold-wall reactors operated at near-atmospheric pressures, fluid flow and gas-phase reactions are important in predicting performance, as discussed earlier in relation to transport phenomena. 

A summary of hydrodemetallation kinetic studies is presented in Table XXVI. The list is not exhaustive but does include a diversity of feedstocks and catalysts. It is apparent that a discrepancy in reaction order rt with respect to total metal (Ni or V) concentration has been observed. Riley (1978) reported first-order kinetics for both nickel and vanadium removal when hydrotreating a Safaniya atmospheric residuum. Demetallation kinetic order of 1.0 to 1.5 depending on reactor configuration has been reported by van Dongen et al. (1980) for vanadium removal. Oleck and Sherry (1977) report a better description of the reaction system is obtained with second-order kinetics for nickel and vanadium removal from Lago-medio (Venezuelan) atmospheric residuum. All studies were conducted on CoMo/A1203 catalysts. 

Table 11 Summary of the reaction products generated via the deprotonation of styrene oxide 83 in a microflow reactor (RT = 24 s, —78 °C)...

Although a number of the surveys listed in Table II (e.g. 6,11,13,16-18) provide a treatment of polymerization reactors and processes in industrial use, Gerrens has provided an outstanding summary of this information in his recent survey (18). Table VII, taken from Gerrens1 review provides an indication of the variety of reactor configurations found in industrial practice. 

Table 13.8 Summary of design and operating procedure for two polymerization reactors.

Table 1. Summary of relative reactor ratings (L = low, M = medium, H = high).

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