D reactors

Figure 1. Typical reactor temperature profile for continuous addition polymerization a plug-flow tubular reactor. Kinetic parameters for the initiator 1 = 10 ppm Ea = 32.921 kcal/mol In = 26.492 In sec f = 0.5. Reactor parameter [(4hT r)/ (DpCp)] = 5148.2. [(Cp) = heat capacity of the reaction mixture (p) = density of the reaction mixture (h) = overall heat-transfer coefficient (Tf) = reactor jacket temperature (r) = reactor residence time (D) = reactor diameter].

T = temperature p = density AH = heat of reaction h = heat-transfer coefficient D = reactor diameter Cp = heat capacity Rp = polymerization rate Tj = reactor jacket temperature P = pressure... 

On September 13, 1944, the Hanford Site started the B Reactor. For approximately 1 hour all went well, but the reactor malfunctioned as a result of fission product poisons. On December 17, 1944, the Hanford Site D reactor was started and the B reactor was repaired and restarted. Large-scale plutonium production was under way. On February 25, 1945, the Hanford F Reactor was started. With these three reactors operating simultaneously, the theoretical plutonium production capacity was approximately 21 kilograms per month. 

For the case of impossible 3-D reactor or vessel sampling, this upward-flowing pipeline sampler should be implemented with the reactor in a recirculation loop configuration, as shown in Figure 3.20. The only new requirement is a low-power pump, to be operated full-time for all systems where this is feasible. 

Figure 1. Copolymerization purging apparatus and reactor with attached dila-tometers initiator ampule (I) dilatometers (D) reactor (R) purging solution collector (P) n-butyllithium in hexane solution (N).

Figure 10. Reaction chromatograms for A, Amstel river water and B, Amstel river water fortified with 3 ng of aldicarb (peak 1) 3 ng of methomyl (peak 2) 5 ng of propoxur (peak 3) 5 ng of carbaryl (peak 4) and 10 ng of methiocarb (peak 5). Conditions 150-mm X 4.6-mm i.d. column packed with Spherisorb ODS mobile phase of 50% water and 50% methanol (v/v) at a flow rate of 1.0 mL/min 60-mm X 4.6-mm i.d. reactor column packed with Aminex A-28 reaction temperature of 100 °C OF A reagent flow rate of 30 pL/min detection with Perkin-Elmer Model 204A fluorescence spectrometer excitation wavelength of 340 nm emission wavelength of 455 nm. (Reproduced with permission from reference 46. Copyright 1983 Elsevier Scientific Publishers.)...

Figure 17.23. Representative temperature profiles in reaction systems (see also Figs. 17.20, 17.21(d), 17.22(d), 17.30(c), 17.34, and 17.35). (a) A jacketed tubular reactor, (b) Burner and reactor for high temperature pyrolysis of hydrocarbons (Ullmann, 1973, Vol. 3, p. 355) (c) A catalytic reactor system in which the feed is preheated to starting temperature and product is properly adjusted exo- and endothermic profiles, (d) Reactor with built-in heat exchange between feed and product and with external temperature adjustment exo- and endothermic profiles.

The D-T reactor is technologically more complex than the D-D reactor because of ihe need to facilitate the second reaction (which takes place outside the plasma) and because very energetic neutrons must be slowed down to allow the reaciion with lithium to lake place. However, the conditions needed to achieve net power output are less demanding than for the D-D fuel reactor. The D-T reaciion will probably be exploited first, but its ultimate, very long term use may be limited by the availability of lithium. 

Schematic of SDR system Lid with viewing windows Spinning Disc, diameter D Reactor Vessel Injector (with stirrer option)...

Glasser D, Hildebrandt D. Reactor and process synthesis. Comput Chem Eng 1997 21 775. 

A, = jacket heat transfer area (m2) = 7rDL D = reactor diameter (m)... 

I OiamelH Yari along btelaigihot D reactor rTubetiw kendK... 

Vertical Scale-Up of Fluid Bed. The fluid-bed process was first scaled up vertically from the 45 cm tall bench-scale reactor to the 760 cm tall 4 B/D reactor shown schematically in Figure 11. The 4 B/D reactor internal diameter was 10 cm. 

Fig. 4. Schematic diagram of a concentric-tube airlift bioreactor (with working volume of 1.0 1). 1 Reactor column 2 inner draft tube (with its height of 15 cm) 3 sparger B bottom clearance (2.5 cm) d diameter of draft tube (4.5 cm) D reactor diameter (7.0 cm) H column height (40 cm)...

Figure 8. Pyrrhotites from reactors 10 Ib/d reactor (A) and 400 Ib/d reactor (%).

Figure 19. Gas-phase polymerization of ethylene (Unipol process) [2] (a) compressor, (b) cooler, (c) catalyst feed hopper, (d) reactor, (e) separator...

Hickman, D.A. and Schmidt, L.D. Reactors, kinetics and catalysis—Steps in CH4 oxidation on Pt and Rh surfaces High-temperature reactor simulations. AIChE Journal, 1993, 39 (7), 1164. 

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