Abstract: The product effluent of a Fischer-Tropsch synthesis is subjected to cooling sufficient to separate a high boiling product fraction boiling above about 400.degree. F from lower boiling product effluent material and comprising water product with formed oxygenates. The total lower boiling product effluent thus obtained is passed in contact with a special class of selective crystalline zeolite catalyst maintained under conditions to improve upon the hydrocarbon products contacted and convert oxygenates for hydrocarbons.

Abstract: The product of Fischer-Tropsch Synthesis is separated to recover a product boiling above and below about 400.degree. F which is thereafter separately process over different beds of ZSM-5 crystalline zeolite under conditions promoting the formation of fuel oil products and gasoline of a higher octane rating.

Abstract: The total product effluent of Fischer-Tropsch synthesis separated from catalyst fines is passed in contact with a crystalline zeolite catalyst represented by ZSM-5 before separation into desired product fractions and C.sub.5 minus gaseous products are catalytically converted to gasoline boiling components.

Abstract: The product of Fischer-Tropsch Synthesis is separated to recover a C.sub.5 -400.degree. F liquid fraction which is thereafter contacted with a ZSM-5 type zeolite in the presence of added hydrogen under conditions of elevated temperature and pressure so as to obtain gasoline of a higher octane rating.

Abstract: Catalyst and hydrocarbon vapors are separated in a cyclone attached to the discharge of a riser cracking operation. The cyclone is modified to include a separate cyclonic stripping of catalyst separated from hydrocarbon vapors.

Abstract: Upgrading of Fischer-Tropsch synthesis product is accomplished by water washing the product effluent to separate oxygenates therefrom, separating the washed effluent to recover a C.sub.3 -C.sub.4 rich fraction, a C.sub.5 plus gasoline fraction, a light fuel oil fraction and a heavy fuel oil fraction which is subjected to hydrodewaxing conditions to produce additional light fuel oil and gasoline boiling product. The light fuel oil products were hydrotreated and the synthesis gasoline is octane improved with ZSM5 crystalline zeolite.

Abstract: Upgrading a fraction of a heavy Fischer-Tropsch oil to jet fuel by hydropretreating a 350.degree. to 850.degree. F boiling fraction; separating the hydrotreated product into a 650.degree. F minus and a 650.degree. F plus fraction, separating the650.degree. F minus fraction to provide a 350.degree. F minus naphtha boiling range fraction and a 350.degree. to 650.degree. F light distillate fraction; distilling the 350.degree. to 650.degree. F hydrotreated fraction to provide a fraction boiling in the range of 350.degree. F to 550.degree. F separate from a 550.degree. to 650.degree. F fraction processing either of the 650.degree. F plus fraction above separated or the 350.degree. to 550.degree. F boiling fraction above obtained over a catalyst comprising a crystalline aluminosilicate zeolite having a silica to alumina ratio of at least 12 and a constraint index of 1 to 12 with hydrogen, at a temperature of about 500.degree. to 800.degree.

Abstract: The conversion of methanol to gasoline boiling hydrocarbons in a thermally balanced operation with a special group of zeolite catalysts having a constraint index of 1 to 12, a silica to alumina ratio of at least about 12 and a crystal density of not substantially lower than about 1.6 grams per cubic centimeter is described. The steady state operation of the process is improved by feeding methanol preheated to a selected temperature proximate to its boiling point so that the heat required thereafter to vaporize the feed and to raise its temperature to conversion temperature is substantially equal to the exothermicity of the conversion itself.

Abstract: Upgrading of Fischer-Tropsch synthesis product is obtained by separating a 560.degree. F minus hydrocarbon fraction from gaseous C.sub.5 rich material and a water phase comprising oxygenates. Alcohols may be recovered from the water phase for conversion to gasoline boiling components. C.sub.5 rich material is converted to gasoline boiling material with a ZSM-5 crystalline zeolite and upgrading of the 560.degree. F minus hydrocarbon fraction is accomplished with a ZSM-5 crystalline zeolite catalyst.

Abstract: A combination process is provided for upgrading 650.degree. F minus product of Fischer-Tropsch Synthesis to provide high yield of high octane gasoline along with improved yields of light fuel oil product. Polymerization and alkylation of C.sub.5 minus gaseous material provide products suitable for blending with gasoline and fuel oil product. A ZSM5 catalyst is relied upon to improve the octane rating of C.sub.5 plus gasoline product of an end point within the range of about 320.degree. F up to about 430.degree. F.

Abstract: A combination process is provided which upgrades the C.sub.3 to 650.degree. F product of Fischer-Tropsch Synthesis to form gasoline product of improved octane rating by contact with ZSM-5 crystalline zeolite and hydrogenation of light fuel oil to improve its stability and color characteristics. Gaseous products are converted to alkylate in the gasoline boiling range. The yield of light fuel oil may be increased by reducing the end point of the gasoline fraction to about 320.degree. F.

Abstract: A Fischer-Tropsch synthesis effluent is separated into gaseous, gasoline boiling, light fuel oil and heavy fuel oil products for upgrading to more desirable products by conversion over a special class of crystalline zeolites suitable for the purpose. Water washing of the separated fractions may be practiced to recover oxygenates from any separated fraction before further upgrading of oxygenates and hydrocarbons.

Abstract: A hydrocarbon conversion-catalyst regeneration operation is described which relies upon a dense fluid catalyst bed superimposed by a dispersed catalyst phase operation to effect elevated temperature regeneration of the catalyst providing low CO levels less than 0.15 mol percent in the flue gas by mixing regenerated catalyst with spent catalyst to obtain an initial mix temperature of at least 1175.degree. F. before contact with oxygen containing regeneration gas. The ratio of regenerated to spent catalyst is restricted to within the range of 0.5 to 1.5 and the oxygen content through the dense and dispersed catalyst phase is selected to provide a discharged dispersed catalyst phase temperature of at least 1350.degree. F.

Abstract: This invention provides a process which involves solubilizing coal in a thermally stable refinery petroleum solvent to form a homogeneous solution, and blending the homogeneous solution with petroleum cutter-stock to produce No. 5 fuel oil.

Abstract: An operation is described which involves the catalytic cracking of high boiling hydrocarbons in the presence of hydrogen and carbon-hydrogen contributing fragments in the presence of particularly crystalline zeolite conversion catalysts promoting the chemical reactions of cracking, hydrogen redistribution, olefin cyclization and chemical reactions providing mobile hydrogen in one of several different forms and suitable for completing desired hydrogen transfer reactions. The chemical reactions desired are particularly promoted by a mixture of large and smaller pore crystalline zeolites in the presence of hydrogen contributing materials such as methanol or mixed with one or more reactants which will form methanol under suitable reaction conditions.

Abstract: The conversion of methanol to gasoline boiling products in a plurality of sequentially arranged catalyst beds comprising a dehydration catalyst followed by a special class of crystalline zeolite conversion catalyst is described wherein the dehydration catalyst life is prolonged and durene formed in the process is recycled to the zeolite catalyst conversion step.

Abstract: This invention provides an improved process for solvent-refining coal which involves heating an admixture of coal and a thermally stable organic solvent to solubilize substantially the coal to form a slurry of liquefaction phase and a residual solids phase, and thereafter passing the slurry through a filter bed of crushed raw coal to separate the liquefaction phase from the solids phase.

Abstract: A process is disclosed for upgrading a naphtha which has been subjected to a reforming process which involves contacting said reformed naphtha together with added hydrogen with a crystalline aluminosilicate zeolite having a pore size of about 4.5 to 6 Angstrom units and a silica to alumina ratio of at least 3, said aluminosilicate having hydrogenation/dehydrogenation activity. Another embodiment of the invention resides in mixing a reforming catalyst with said crystalline aluminosilicate zeolite.

Abstract: A combination operation is described comprising gas oil cracking in the presence of a large and smaller pore size crystalline zeolite dual component cracking catalyst in which combination C.sub.6 minus products are separated and catalytically upgraded under selected conditions providing cyclization and/or carbon chain growth as by oligmerization and polymerization. Conversion of C.sub.6 and lower boiling hydrocarbons is particularly accomplished with the smaller pore crystalline zeolite of the dual component catalyst.

Abstract: A process is disclosed in which pyritic sulfur in coals is removed by treatment with aqueous solutions containing manganese, vanadium and cerium metal oxidants.