Abstract: This invention relates to the synthesis of large pore composite molecular sieves and to the synthetic large pore composite molecular sieves so produced. The molecular sieves of the invention have the same general utilities of the comparable molecular sieves of the prior art but have been found to be superior catalysts and absorbents. This invention relates to a hydrothermal synthesis of large pore molecular sieves from nutrients, at least one of which contains an amorphous framework-structure, and which framework-structure is essentially retained in the synthetic molecular sieve. This invention stems from a discovery that the intrinsic porosity characteristics of a nutrient that possesses an amorphous cation oxide-framework can be substantially retained in the final molecular sieve containing product formed by a hydrothermal process by carefully controlling the conditions under which the hydrothermal process is conducted.

Abstract: A porous composite product comprised of a network of fibers is produced by forming an unsintered preformed network of fibers and a gasifiable structure forming agent, followed by gasification of the structure forming agent prior to sintering of the fibers at appropriate junction points. The preferred structure forming agent is a cellulosic material.

Abstract: This invention relates to the synthesis of large pore composite molecular sieves and to the synthetic large pore composite molecular sieves so produced. The molecular sieves of the invention have the same general utilties of the comparable molecular sieves of the prior art but have been found to be superior catalysts and absorbents. This invention relates to a hydrothermal synthesis of large pore molecular sieves from nutrients, at least one of which contains an amorphous framework-structure, and which framework-structure is essentially retained in the synthetic molecular sieve. This invention stems from a discovery that the intrinsic porosity characteristics of a nutrient that possesses an amorphous cation oxide-framework can be substantially retained in the final molecular sieve containing product formed by a hydrothermal process by carefully controlling the conditions under which the hydrothermal process is conducted.

Abstract: Useful cracking catalysts and catalyst supports comprising a mixture of tungsten oxide and silica supported on a boehmite-like surface which, in turn, is supported on alumina are prepared by forming a composite of particles of (a) tungsten oxide, (b) silica and (c) boehmite and subjecting the composite to steaming at a temperature of at least about 500.degree. C. During the steaming, the tungsten oxide and silica react with the surface of the boehmite as the boehmite converts to alumina.

Abstract: Useful cracking catalysts and catalyst supports comprising silica supported on alumina are prepared by compositing particles of silica or silica precursor with particles of porous alumina and subjecting the resulting composite to high temperature steaming in a non-reducing environment at a temperature of at least about 500.degree. C. for a time sufficient to disperse at least a portion of the silica over the alumina surface. The silica wets, spreads out and reactions with the surface hydroxyul groups of the alumina. The supported silica on alumina composites that can be made from this process may exhibit properties of both bulk silica and bulk alumina at the same time, bulk silica and alumina whose exterior surface only has been modified with silica as wells as composites exhibiting surface properties different from both bulk silica and bulk alumina.

Abstract: Useful cracking catalysts and catalyst supports comprising silica supported on a boehmite-like surface are prepared by compositing particles of silica or hydrated silica with particles of porous boehmite and subjecting the resulting composite to high temperature steaming at a temperature of at least about 600.degree. C. for a time sufficient to disperse at least a portion of the silica over the boehmite surface as the boehmite converts to .gamma.-Al.sub.2 O.sub.3. The silica wets, spreads out and reacts with the surface hydroxyl groups of the transforming boehmite.

Abstract: Useful cracking catalysts and catalyst supports comprising mixtures of tungsten oxide and silica supported on alumina are prepared by forming a composite of a mixture of (a) particles of tungsten oxide or one or more suitable tungsten oxide precursors, (b) particles of silica and (c) particles of porous alumina and steaming said composite at a temperature of at least about 500.degree. C. in a non-reducing environment for a time sufficient for at least a portion of the tungsten oxide and silica to disperse over the alumina surface. The mixture of silica and tungsten oxide wets, spreads out and reacts with the surface hydroxyl groups of the alumina.

Abstract: A process for removing metal contaminants from a hydroconversion catalyst, said catalyst containing at least one metal from Groups VIB, VIIB or VIII supported on a refractory inorganic oxide. The process comprises contacting the contaminated catalyst with a buffered oxalic acid solution wherein contaminant is removed without dissolving the support.

Abstract: Acid catalysts comprising a catalytic metal oxide component wherein said metal is selected from the group consisting essentially of (a) tungsten, niobium and mixtures thereof and (b) mixtures of (a) with tantalum, hafnium, chromium, titanium, zirconium and mixtures thereof, supported on a silica-containing inorganic refractory metal oxide support support wherein the silica content thereof is less than 50 wt. % of the total support, said catalyst being steamed prior to use at a temperature at least 600.degree. C. In a preferred embodiment, the support will comprise a mixture of silica and the .gamma.-alumina wherein the silica content is less than 25 wt. % thereof.

Abstract: Basic asphaltenes are selectively removed from asphaltene-containing hydrocarbon feeds by contacting the feed with a transition metal oxide solid acid catalyst which selectively adsorbs the basic asphaltenes. The catalyst will comprise a catalytic metal component selected from the group consisting essentially of oxides of (a) tungsten, niobium, and mixtures thereof and (b) mixtures of (a) with tantalum, hafnium, chromium, titanium, zirconium and mixtures thereof, supported on an inorganic refractory oxide support such as alumina. Asphalt-laden catalyst is separated from the feed, the asphaltenes adsorbed thereon are cracked off in the presence of steam and the catalyst is regenerated and recycled back to the adsorption zone.

Abstract: Basic asphaltenes are selectively removed from asphaltene-containing hydrocarbon feeds by contacting the feed with a transition metal oxide solid acid catalyst exhibiting Bronsted acidity. The catalyst selectively adsorbs the basic asphaltenes. The catalysts will comprise a catalytic metal component selected from the group consisting essentially of oxides of (a) tungsten, niobium and mixtures thereof and (b) mixtures of (a) with tantalum, hafnium, chromium, titanium, zirconium and mixtures thereof, supported on pyrogenic alumina. Asphalt-laden catalyst is separated from the feed, the asphaltenes adsorbed thereon are cracked off in the presence of steam and the catalyst is regenerated and recycled back to the adsorption zone.

Abstract: Hydrocarbons are cracked by contacting, in a cracking zone and at elevated temperature, a hydrocarbon feed with an acid catalyst comprising at least a catalytic metal oxide component wherein said metal is selected from the group consisting essentially of (a) tungsten, niobium and mixtures thereof and (b) mixtures of (a) with tantalum, hafnium, chromium, titanium, zirconium and mixtures thereof, and wherein said catalytic metal oxide component is supported on a silica-containing inorganic refractory metal oxide support the silica content of which is less than 50 wt. % of the total support, said catalyst being steamed prior to use at a temperature at least 600.degree. C. In a preferred embodiment, the support will comprise a mixture of silica and the .gamma.-alumina wherein the silica content is less than 25 wt. % thereof. Further, one may employ steam in the cracking zone.

Abstract: Hydrocarbons are cracked by contacting same, at elevated temperature with a solid acid catalyst having primarily Bronsted acidity which comprises at least one catalytic metal oxide component selected from the group consisting essentially of oxides of (a) tungsten, niobium and mixtures thereof and (b) mixtures of (a) with tantalum, hafnium, chromium, titanium, zirconium and mixtures thereof, supported on pyrogenic alumina. The exceptional high temperature steam stability of these catalysts permits the use of steam in the reaction zone, if desired.

Abstract: Solid acid catalysts having primarily Bronsted acidity which comprise at least one catalytic metal oxide component selected from the group consisting essentially of oxides of (a) tungsten, niobium and mixtures thereof and (b) mixtures of (a) with tantalum, hafnium, chromium, titanium, zirconium and mixtures thereof, supported on pyrogenic alumina. These catalysts are useful cracking catalysts and have exceptional high temperature steam stability.

Abstract: An acid catalyst comprising a catalytic component selected from the group consisting of oxides of tungsten, niobium and mixtures thereof and tungsten or niobium oxides in combination with one or more additional metal oxides selected from the group consisting of tantalum oxide, hafnium oxide, chromium oxide, titanium oxide and zirconium oxide on an inorganic refractory oxide support is prepared by depositing by means known in the art a metal oxide precursor salt on an inorganic refractory metal oxide which is not itself an acid cracking catalyst or by intimately mixing a metal oxide precursor salt with a refractory metal oxide support precursor salt, converting the salt or salts to the respective metal oxides and subjecting the resultant combination to steaming at elevated temperatures prior to use. Catalysts prepared in this manner exhibit enhanced activity and selectivity as compared to conventional acid catalysts. They also exhibit remarkable resistance to coke make.

Abstract: Novel .omega.alkenyl silane monoadducts and bis-.alpha., .omega.-silyl alkanes are disclosed. The .omega.-alkenyl silanes or bis-.alpha.,.omega.-silyl alkanes are prepared by the selective addition of silane having chlorine, alkoxy or acyloxy groups to an .alpha.,.omega.-diene. The additions may be carried out in the liquid phase in the presence of free radical and/or metal and/or metal salt catalyst.

Abstract: It has been discovered and forms the basis of the disclosure that various acid catalyzed hydrocarbon conversion processes such as catalytic cracking of gas oil; xylene isomerization; toluene disproportionation; dealkylation of aromatics; ethylene, butylene, isobutylene, propylene polymerization; olefin isomerization; alcohol dehydration; olefin hydration; alkylation; heavy ends cat cracking, etc. are dramatically improved insofar as percent conversion, and selectivity are concerned by the use of a catalyst selected from the group consisting of the oxides of tungsten, niobium and mixtures thereof, and tungsten or niobium oxides in combination with one or more additional metal oxides selected from the group consisting of tantalum oxide, hafnium oxide, chromium oxide, titanium oxide and zirconium oxide, supported on an inorganic refractory oxide support. These catalysts may be prepared by the methods known in the art, i.e., incipient wetness, impregnation, coprecipitation, etc.

Abstract: Novel heterogeneous silylhydrocarbyl phosphine transition metal complex catalysts and intermediates therefor are prepared by (a) the selective monoaddition of silane having chlorine, alkoxy or acyloxy groups to an .alpha., .omega.-diene, (b) followed by the addition of a phosphine to the resulting .omega.-alkenyl silanes to form the corresponding silylalkyl phosphines, (c) which are then covalently anchored as such or in the form of their transition metal complexes via condensation of their reactive silane substituents with hydroxy groups of silica and metal oxides, (d) optionally followed by complexing the free phosphine groups of anchored silylalkyl phosphines with transition metal compounds.

Abstract: The preparation of an ultra-stable, high surface area alpha-alumina catalyst and catalyst support suitable for use in high temperature processes such as petroleum refining processes, e.g., resid cat cracking and steam reforming, is disclosed. The process comprises impregnating high surface area gamma-alumina having narrow pores with a carbonaceous material that readily chars to form carbon. The impregnated alumina is then heated to a temperature sufficient to induce charring, following which the gamma-alumina is converted to alpha-alumina by further heating. The carbon is subsequently removed by oxidation. The alpha-alumina thus produced can withstand temperatures up to at least about 1000.degree. C. in the presence of steam without substantial loss of surface area.

Abstract: The instant invention relates to a method for preparing high activity supported nickel catalysts. The method comprises the deposition of nickel nitrate on a carrier, typically an inert inorganic refractory oxide, by techniques known in the art followed by careful heating to a temperature of between 100.degree. to 270.degree. C., avoiding any excursions into temperatures beyond the stated maxima, in a flowing nonreactive gas atmosphere for a time sufficient to convert substantially all of the nickel nitrate into nickel oxide. When using an H.sub.2 containing atmosphere the maximum temperature is 220.degree. C. The supported nickel oxide resulting from the above procedure is then reduced to a supported nickel metal catalyst in a reducing atmosphere at a temperature ranging from about 230.degree. C. to 400.degree. C.