Gas reactors for

A group studying High Temperature Gas Reactor for enhance oil recovery in 1987 has become a team dedicated for high temperature reactor since 1993. 

Yan, X., Sato, H., Tachibana, Y., Kunitomi, K., Hino, R., 2012a. Evaluation of high temperature gas reactor for demanding cogeneration load follow. Journal of Nuclear Science and Technology 49 (1), 121-131. 

Reference 4 1 included a best estimate mass of approximately 6,500 kg for the 4-4-4 system. This mass was calculated by NRPCT using an extrapolation from a NASA Glenn mass estimating tool (SRPS Opt) substituting a gas reactor for the liquid lithium reactor used by NASA. This compares with a current best estimate mass for a 4-4-4 system of 11,300 kg. This is an increase in estimated mass of 4,750 kg. Figure 4-2 shows a graphical representation of the masses of the current 4-4-4 system and the mass reported in the concept selection r ort for the same system. 

In the one-stage process (Fig. 2), ethylene, oxygen, and recycle gas are directed to a vertical reactor for contact with the catalyst solution under slight pressure. The water evaporated during the reaction absorbs the heat evolved, and make-up water is fed as necessary to maintain the desired catalyst concentration. The gases are water-scmbbed and the resulting acetaldehyde solution is fed to a distUlation column. The tad-gas from the scmbber is recycled to the reactor. Inert materials are eliminated from the recycle gas in a bleed-stream which flows to an auxdiary reactor for additional ethylene conversion. 

The gas leaving the heat recovery equipment contains soot and ash some ash is deposited in the bottom of the reactor for removal during periodic inspection shutdowns. The gas passes to a quench vessel containing multiple water-sprays which scmb most of the soot from the gas. Additional heat recovery can be accompHshed downstream of the quench vessel by heat exchange of the gas with cold feed water. Product gas contains less than 5 ppm soot. 

Conoco operated a stirred tank Pfaudler glass-lined reactor for the batch SO sulfonation of detergent alkylate. The plant utilized over-the-fence SO converter gas (8% SO ia dry air) having h batch cycles (264). AHied Chemical Company provided details for batch SO sulfonation (265,266)... 

Types ofSCT Catalysts. The catalysts used in the SCR were initially formed into spherical shapes that were placed either in fixed-bed reactors for clean gas apphcations or moving-bed reactors where dust was present. The moving-bed reactors added complexity to the design and in some appHcations resulted in unacceptable catalyst abrasion. As of 1993 most SCR catalysts are either supported on a ceramic or metallic honeycomb or are direcdy extmded as a honeycomb (1). A typical honeycomb block has face dimensions of 150 by 150 mm and can be as long as one meter. The number of cells per block varies from 20 by 20 up to 45 by 45 (39). 

Many configurations of laboratory reactors have been employed. Rase (Chemical Reactor Design for Proce.s.s Plants, Wiley, 1977) and Shah (Ga.s-Liquid-Solid Reactor Design, McGraw-Hill, 1979) each have about 25 sketches, and Shah s bibliography has 145 items classified into 22 categories of reactor types. Jankowski et al. (Chemlsche Tech-nik, 30, 441 46 [1978]) illustrate 25 different lands of gradientless laboratory reactors for use with solid catalysts. 

Loop Reactors For some gas-hquid-solid processes, a recirculating loop can be an effective reactor. These involve a relatively high horsepower pumping system and various kinds of nozzles, baffles, and turbulence generators in the loop system. These have power levels... 

FIG. 23-41 Gas/liqi lid fluidized (ehiillartng) hed reactor for hydroliqiiefac6on of coal. (Kampiner, in Winnacker-Keuchler, Chemische Technologic, vol. 3, Hanser, 1972, p. 252. )... 

Status of Indirect Liquefaction Technology The only commercial indirect coal liquefaction plants for the production of transportation fuels are operated by SASOL in South Africa. Construction of the original plant was begun in 1950, and operations began in 1955. This plant employs both fixed-bed (Arge) and entrained-bed (Synthol) reactors. Two additional plants were later constructed with start-ups in 1980 and 1983. These latter plants employ dry-ash Lurgi Mark IV coal gasifiers and entrained-bed (Synthol) reactors for synthesis gas conversion. These plants currently produce 45 percent of South Africa s transportation fuel requirements, and, in addition, they produce more than 120 other products from coal. 

Eastman Chemical Company has operated a coal-to-methanol plant in Kingsport, Tennessee, since 1983. Two Texaco gasifiers (one is a backup) process 34 Mg/h (37 US ton/h) of coal to synthesis gas. The synthesis gas is converted to methanol by use of ICl methanol technology. Methanol is an intermediate for producing methyl acetate and acetic acid. The plant produces about 225 Gg/a (250,000 US ton/a) of acetic anhydride. As part of the DOE Clean Coal Technology Program, Air Products and Cnemicals, Inc., and Eastman Chemic Company are constructing a 9.8-Mg/h (260-US ton/d) slurry-phase reactor for the conversion of synthesis gas to methanol and dimethyl... 

Lackey, W.J., Stinton, D.P. and Seasc, J.D., Improved gas distribution for coating high-temperature gas-ceioled reactor fuel particles. Nuclear Technology, 1977, 35, 227 237. 

Following are examples for finding die time of an isodiermal batch reactor for a given conversion of die reactant and odier pertinent variables, and for gas phase reaction. 

Figure 8.11 Types of reactors for gas-liquid precipitation, (a) bubbling stirred tank, (b) fiat interface stirred tank, draft-tube bubble column, (d) spray column after Wachi and Jones, 1994)...

Figure 10-9. The UOP (Detal) process for producing linear alkylbenzene (1) pacol dehydrogenation reactor, (2) gas-liquid separation, (3) reactor for converting diolefins to monoolefins, (4) stripper, (5) alkylation reactor, (6,7,8) fractionators.

The separation of the excess unreacted sodium is also subject to investigation and development. Miyazaki and Kuroki [588] proposed a reactor system for the reduction of K2TaF7 or K2NbF7 with Na or K, respectively. According to this method, the reduced melt is tapped into a special chamber for solidification, while unreacted Na or K is trapped with a condenser in the gas phase for recycling. 

Gas hold-up is defined as volume of gas per unit volume of reactor. For ah in water, Richard s data are by ... 

The chapter by Haynes et al. describes the pilot work using Raney nickel catalysts with gas recycle for reactor temperature control. Gas recycle provides dilution of the carbon oxides in the feed gas to the methanator, hence simulating methanation of dilute CO-containing gases which under adiabatic conditions gives a permissible temperature rise. This and the next two papers basically treat this approach, the hallmark of first-generation methanation processes. 

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