C-Reactor

As an example, the battery-limits capital cost can be estimated for the production of 10,000 t/yr of ethylene (qv) from ethanol (11). Seven processing blocks, ie, vaporizer, reactor, water quench, compressor, dryer, distillation, and energy recovery, can be identified. The highest temperature is 350°C (reactor), and the highest pressure is about 1.7 MPa (17 atm) (compressor, two towers). If a materials-pressure factor, + of 1.03 is assumed, then for N = 7 0 = 0.87 1/0 = 1 64 and f =0 K = 6.3. This gives the 1981 cost as 4.4 X 10 . The 1991 battery-Hmits investment can be obtained, by updating with the CE Plant Cost Index, as 5.3 x 10 . ... 

Selectivity may also come from reducing the contribution of a side reaction, e.g. the reaction of a labile moiety on a molecule which itself undergoes a reaction. Here, control over the temperature, i.e. the avoidance of hot spots, is the key to increasing selectivity. In this respect, the oxidative dehydrogenation of an undisclosed methanol derivative to the corresponding aldehyde was investigated in the framework of the development of a large-scale chemical production process. A selectivity of 96% at 55% conversion was found for the micro reactor (390 °C), which exceeds the performance of laboratory pan-like (40% 50% 550 °C) and short shell-and-tube (85% 50% 450 °C) reactors [73,110,112,153,154]. 

Operating temperature 370 °C Reactor No. 4 total number of reaction channels 20... 

Solution feed rate 14.2 cm3/sec Inlet feed temperature 25 °C Reactor volume 2790 cm3... 

Rasmussen, N.C. Reactor Safety Study WASH-1400. U.S. Nuclear Regulatory Commission, 1975. 

After a demonstration at the Hanford Site C Reactor in 1998, the DOE estimated that it would cost approximately 50,000 to remediate the 1956 contaminated lead bricks on site. Costs would range from 0.96 per pound if the bricks were presurveyed for contamination levels to 0.99 per pound if the bricks were not presurveyed. The presurveying option is less expensive because not all of the bricks would require decontamination. These estimates do not include money earned from the salvage value of the bricks (D198327, pp.l6, 17). The DOE notes that TechXtract was not cost effective at Hanford due to the cheap costs of landfill disposal at the facility (D222719, p. 6). 

Trichloroethene (0.69mol h ). 2-chloro-l,l.l-trifluoroelhene (0.17 mol h ) and IIF (5.14mol li" ) were led to a 300 C reactor packed with a catalyst prepared from fluorinated alumina which had been treated with CrCI,. After a contact time of 5 s, trichloroethene was converted with no sign of catalyst degradation after 70h. 2-Chloro-l.l,l-trifluoroethene was formed yield 94%. 

Methylene dichloride and chloroform may be produced by modified methods using a mixture of chlorine, methane, and methyl chloride as feed. Chlorination is run at 350-400°C reactor temperature at slightly above atmospheric pressure. A 2.6 1 chlorine methane ratio results in an optimal yield of chloroform. Alternatively, excess methane is reacted with chlorine at 485-510°C to produce methylene dichloride as the main product.181 The predominant method, however, still is the chlorination of methyl chloride manufactured by the reaction of methyl alcohol and hydrogen chloride.181... 

Fig. 14.12 Stack concentrations of UHC as function of NO in the exhaust of a lean-burn natural gas fired engine [234], The following conditions can be assumed for the exhaust system inlet composition CH4 = 4410 ppm, C2H6 = 490 ppm, O2 = 8.5%, H2O =13%, CO2 = 6.5%, NO = 10-1813 ppm, NO2 = 3-544 ppm, balance nitrogen temperature = 680°C, reactor residence time = 210 ms, pressure = 1.7 bar.

Figure 50. Furnace black reactors A) Restrictor ring reactor B) Venturi reactor [4.15] C) Reactor with high-speed combustion chamber [4.16]...

Table 14.15 shows the values for H202/UV-C oxidation of the reactive dye bath effluent in the photochemical (UV-C) reactor in the presence of 680 mg/ L H202 at varying pH values. Table 14.15 shows that kd and uv280 values increased by factors of 2.7 and 2.6, respectively, by elevating the pH from 3 to 7. Overall fcUV280 removal efficiency was not seriously affected by the reac-... 

Figure 6.10 Example substitution reaction in the Isoperibolic batch reactor starting from 25°C with a constant cooling system temperature (Tc) at 25 °C. Reactor temperature (T,°C) and conversion as a function of time (h).

Copper salt Reducing agent Temperature °C Reactor Mean size of product, nm Reference... 

If the desired product is C, reactor temperature should be selected so that the specific reaction rate k of the desired reaction is large compared to the specific reaction rate k2 of the undesired reaction. If the orders of reactions are different in terms of their dependence on the two reactants, the concentrations can also be adjusted to favor the desired reaction ... 

At 25-26 °C reactor 10 receives mixture II from batch box 9 at such speed that the temperature in the apparatus does not exceed 26°C. After all mixture II is added, the reactive mixture is heated, first to 30-35 °C, then (after 3.5-4 hours of standing) to 45-50 °C. At this temperature the mixture also stands for 3.5-4 hours then it is cooled to 20 °C with water sent into the jacket. 

When the medium becomes acid, at 45-48 °C reactor 1 receives a calculated amount of poisonous methanol from batch box 6 at such speed that the temperature in the reactor does not exceed 50°C. Then, at 67-75 °C the released methylacetate is sent from reactor 1 through cooler 7 into neutraliser 8 with an agitator. 

Subsequent to termination of first cycle, refinery carried out the regeneration of catalyst. Sulfur stripping was performed by circulation of hydrogen in the reaction section at 500-510°C reactor inlet temperature and 5 to 7 kg/cm2 separator pressure. Initially H2S... 

Figure 2. Schemes of fixed-bed reactors operated under forced unsteady-state conditions (a) Reverse-flow reactor (b) Rotary reactor (c) Reactor system with periodic changes between the inlet and outlet ports in two fixed beds. The tables show positions of switching valves during two successive cycles C = valve closed O = valve open.

A very facile dip acetylation procedure was developed for wood chips and fibers. The wood is dried at 105°C and then dipped in acetic anhydride for 1 min and drained. Then the sample is placed in a preheated (120°C) reactor for different lengths of time, depending on the degree of substitution of acetyl groups desired in the sample.29 The swelling of aspen flake-board made from such chemically modified flakes is dramatically reduced. For example, while unmodified flakeboard swelled by over 60 percent after immersion in water for 5 days, the modified material swelled by only about 8-22 percent, depending on the extent of chemical modification. 

Flow Rate] [C -C ] = [Reactor Volume] [Reaction Rate] (20)... 

FIGURE 12 Comparison of responses for +30 °C reactor temperature setpoint changes at t = lOmin 500-gal GLCS filled with water (1925kg). 

Using the propyl chlorides as an example (eq. 11, Table II), after five minutes at 140° in a 45 cc Hastelloy C reactor charged with aluminum chloride and 2-chloropropane the pressure was 500 psig of which 71% was propane by mass spectrometric analysis. 

For instance, the engineering hours related to a small or medium sized carbon steel reactor are essentially equal to those related to a larger Hastelloy C reactor. However, the difference in cost can be a full order of magnitude. Engineering hours relate best to the type of equipment and conditions specific to each project. 

C. Reactor effluent—contains all feed and product species at the reactor temperature and pressure. Species partial pressures satisfy the two given equations. 

C. Reactors with Monolithic Palladium-Based Membranes... 

C. Reactors with Metal-Containing Composite Membrane Catalysts... 

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