Steam catalytic

Nazarkina, E. B. and N. A. Kirichenko 1979. Improvement in the steam catalytic conversion of methane by hydrogen liberation via palladium membranes Khim. Tekhnol. Topi. Masel. 3 5-10. 

The concept provides for adiabatic steam catalytic one-stage conversion with carbon dioxide removal through short-cycle heat-free adsorption, followed by return of a part of product fraction to conversion. This option assumes maximum usage of initial hydrocarbon raw material to produce the HMM. 

TECHNICAL AND TECHNOLOGICAL METHODS OF REALIZATION OF STEAM CATALYTIC CONVERSION OF NATURAL GAS WITH A METHANE-WATER PROPORTION CLOSE TO STOICHIOMETRIC RATIO... 

Igumnov V.S., Technical and technological methods of realization steam, catalytic conversion of natural gas with water the ferry. Conference ICHMS 2005, Sevastopol. 

Design Basis. A preliminary design for a multiproduct ioe extraction plant was prepared, based on SCP s proprietary process (Henkel HSaA, op. cit.) and plant design data (Steams Catalytic Corporation, Tolling/Demo SCE Plant, IhlLadelphla, PA, 1984, proprietary data.). Key parameters in the base case design are Feedstock Ibices and herbs (solid)... 

Subsequently, PMCD took over the design program and contracted with Steams Catalytic Corporation to provide the furnaces. The latter utilized Allis Chalmers (now part of Metso Corporation) for the DFSs, Wellman Furnaces Inc. for the MPFs, and T-Thermal Corporation for the LICs. These companies, or their successors, continue to operate and can provide replacement parts as required for the furnaces. Continental Research Engineering (CR E) is a more recently estabhshed company that has personnel who are specialists with over a decade of experience in the operation and maintenance of chemical demilitarization furnaces and who continue to support the four incineration facilities. 

Shattuck, D. M., Ireland, P. A., Keeth. R. J., Mora. R. R., Scheck, R. W., /Vichambeault, J. A., Rathbon, G. R. and Morasky, T. M., 1984, Retrofit FGD Cost-Generating Guidelines. CS-3696, prepared by Steams Catalytic for Electric Power Research Institute, Palo Alto, CA, October. 

Steams Catalytic Corp., 1985, Economic Evaluation of FGD Systems, CS-3342, Vol. 4, Electric Power Research Institute, Palo Alto, CA, July. 

The process may be of practical interest for the steam catalytic conversion of fat natural gases to syngas without preliminary purification from C2+ hydrocarbons or without the stage their preliminary steam prereforming, making it possible to reduce the energy expenditures on the heating of the steam-hydrocarbon mixture. Furthermore, the process may be... 

A greater amount of steam would be generated if the noncondensible vent was treated using catalytic incineration rather than absorption. The... 

Obtained synthetically by one of the following processes fusion of sodium ben-zenesulphonate with NaOH to give sodium phenate hydrolysis of chlorobenzene by dilute NaOH at 400 C and 300atm. to give sodium phenate (Dow process) catalytic vapour-phase reaction of steam and chlorobenzene at 500°C (Raschig process) direct oxidation of cumene (isopropylbenzene) to the hydroperoxide, followed by acid cleavage lo propanone and phenol catalytic liquid-phase oxidation of toluene to benzoic acid and then phenol. Where the phenate is formed, phenol is liberated by acidification. 

The feedstock usually comes from catalytic cracking, sometimes from steam cracking. The reaction products are Cy-Cg isoparaffins. The byproducts are the C3-C4 n-paraffins which do not react. 

Steam reforming is, along with catalytic reforming, a process that can produce the additional hydrogen needed for upgrading and converting the heavy fractions of crude oil. 

In a single stage, without liquid recycle, the conversion can be optimized between 60 and 90%. The very paraffinic residue is used to make lubricant oil bases of high viscosity index in the range of 150 N to 350 N the residue can also be used as feedstock to steam cracking plants providing ethylene and propylene yields equal to those from paraffinic naphthas, or as additional feedstock to catalytic cracking units. 

The catalytic vapor-phase oxidation of propylene is generally carried out in a fixed-bed multitube reactor at near atmospheric pressures and elevated temperatures (ca 350°C) molten salt is used for temperature control. Air is commonly used as the oxygen source and steam is added to suppress the formation of flammable gas mixtures. Operation can be single pass or a recycle stream may be employed. Recent interest has focused on improving process efficiency and minimizing process wastes by defining process improvements that use recycle of process gas streams and/or use of new reaction diluents (20-24). 

There are currentiy two principal processes used for the manufacture of monomeric acryhc esters the semicatalytic Reppe process and the propylene oxidation process. The newer propylene oxidation process is preferred because of economy and safety. In this process acroleia [107-02-8] is first formed by the catalytic oxidation of propylene vapor at high temperature ia the preseace of steam. The acroleia is thea oxidi2ed to acryhc acid [79-10-7]. 

A two-step process involving conventional nonoxidative dehydrogenation of propane to propylene in the presence of steam, followed by the catalytic ammoxidation to acrylonitrile of the propylene in the effluent stream without separation, is also disclosed (65). 

Thermochemical Liquefaction. Most of the research done since 1970 on the direct thermochemical Hquefaction of biomass has been concentrated on the use of various pyrolytic techniques for the production of Hquid fuels and fuel components (96,112,125,166,167). Some of the techniques investigated are entrained-flow pyrolysis, vacuum pyrolysis, rapid and flash pyrolysis, ultrafast pyrolysis in vortex reactors, fluid-bed pyrolysis, low temperature pyrolysis at long reaction times, and updraft fixed-bed pyrolysis. Other research has been done to develop low cost, upgrading methods to convert the complex mixtures formed on pyrolysis of biomass to high quaHty transportation fuels, and to study Hquefaction at high pressures via solvolysis, steam—water treatment, catalytic hydrotreatment, and noncatalytic and catalytic treatment in aqueous systems. 

Cycloaliphatic Diene CPD—DCPD. Cycloatiphatic diene-based hydrocarbon resias are typically produced from the thermal or catalytic polymerization of cyclopeatadieae (CPD) and dicyclopentadiene (DCPD). Upon controlled heating, CPD may be dimerized to DCPD or cracked back to the monomer. The heat of cracking for DCPD is 24.6 kJ / mol (5.88 kcal/mol). In steam cracking processes, CPD is removed from C-5 and... 

Synthesis Gas Chemicals. Hydrocarbons are used to generate synthesis gas, a mixture of carbon monoxide and hydrogen, for conversion to other chemicals. The primary chemical made from synthesis gas is methanol, though acetic acid and acetic anhydride are also made by this route. Carbon monoxide (qv) is produced by partial oxidation of hydrocarbons or by the catalytic steam reforming of natural gas. About 96% of synthesis gas is made by steam reforming, followed by the water gas shift reaction to give the desired H2 /CO ratio. 

Propellant. The catalytic decomposition of 70% hydrogen peroxide or greater proceeds rapidly and with sufficient heat release that the products are oxygen and steam (see eq. 5). The thmst developed from this reaction can be used to propel torpedoes and other small missiles (see Explosives and propellants). An even greater amount of energy is developed if the hydrogen peroxide or its decomposition products are used as an oxidant with a variety of fuels. 

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