Abstract: A method is disclosed for treating gaseous effluent from a hydrocarbon pyrolysis unit to provide steam cracked tar of reduced asphaltene and toluene insolubles content. The method is suitable for preparing reduced viscosity tar useful as a fuel blending stock, or feedstock for producing carbon black, while reducing or eliminating the need for externally sourced lighter aromatics additives to meet viscosity specifications. The method comprises drawing steam cracked tar from a separation vessel, e.g., a primary fractionator or tar knock-out drum, cooling the tar, and returning it to the separation vessel to effect lower overall tar temperatures within the separation vessel, in order to reduce viscosity increasing condensation reactions. An apparatus for carrying out the method is also provided.

Abstract: A method is disclosed for treating gaseous effluent from a hydrocarbon pyrolysis unit to provide steam cracked tar of reduced asphaltene and toluene insolubles content. The method is suitable for preparing reduced viscosity tar useful as a fuel blending stock, or feedstock for producing carbon black, while reducing or eliminating the need for externally sourced lighter aromatics additives to meet viscosity specifications. The method comprises drawing steam cracked tar from a separation vessel, e.g., a primary fractionator or tar knock-out drum, cooling the tar, and returning it to the separation vessel to effect lower overall tar temperatures within the separation vessel, in order to reduce viscosity increasing condensation reactions. An apparatus for carrying out the method is also provided.

Abstract: A method is disclosed for treating gaseous effluent from a hydrocarbon pyrolysis unit to provide steam cracked tar of reduced asphaltene and toluene insolubles content. The method is suitable for preparing reduced viscosity tar useful as a fuel blending stock, or feedstock for producing carbon black, while reducing or eliminating the need for externally sourced lighter aromatics additives to meet viscosity specifications. The method comprises drawing steam cracked tar from a separation vessel, e.g., a primary fractionator or tar knock-out drum, cooling the tar, and returning it to the separation vessel to effect lower overall tar temperatures within the separation vessel, in order to reduce viscosity increasing condensation reactions. An apparatus for carrying out the method is also provided.

Abstract: An integrated process for converting a hydrocarbon feedstock having components boiling above about 100° C. into steam cracked products is described. The process first involves passing the feedstock to a hydrotreating zone to effect substantially complete decomposition of organic sulfur and/or nitrogen compounds. The product from the hydrotreating zone is passed to an aromatics saturation zone. The product is then passed to a steam cracking zone. Hydrogen and C1-C4 hydrocarbons, steam cracked naphtha, steam cracked gas oils and steam cracked tar are recovered. The amount of steam cracked tar produced is reduced by at least about 30 percent, and the amount of steam cracked tar produced is reduced by at least about 40 percent, basis the starting hydrocarbon feedstock which has not been subject to hydrotreating and aromatics saturation.

Abstract: A process for the production of gaseous olefins which involves introducing a hydrocarbon feedstock stream into a high temperature thermal cracking zone to produce a high temperature cracked product stream, quenching the cracked product stream to stop the cracking reactions, injecting at least one HDD (hydrogen donor diluent) into the cracked product stream at or downstream of the point at which the reaction is quenched, recovering normally gaseous olefins from the cracked product stream, and recovering a liquid product stream containing a diminished asphaltene content.

Abstract: A safe, effective, and economical method is provided for recovering olefins from cat-cracked gases without accumulating dangerous amounts of nitrogen oxides. A stream of cat-cracked gas first is scrubbed to remove acid gases, including nitrogen dioxide (NO.sub.2), and then is passed through a depropanizer fractionation tower. Hydrocarbons having four or more carbon atoms are recovered in the bottoms of the depropanizer, and the overhead from the depropanizer--which is composed of hydrocarbons having three or fewer carbon atoms--is sent to an absorber demethanizer tower. Hydrocarbons having two or more carbon atoms are recovered in the bottoms from the absorber demethanizer tower, where temperatures are no lower than about -45.56.degree. C. (-50.degree. F.). The overhead from the absorber demethanizer tower--which is composed of methane, hydrogen, and trace amounts of nitrogen oxide, C.sub.2, and absorbent (C.sub.3)--then is chilled to condense and recover trace amounts of C.sub.

Abstract: A process for the production of gaseous olefins which involves introducing a hydrocarbon feedstock stream into a high temperature thermal cracking zone to produce a high temperature cracked product stream, quenching the cracked product stream to stop the cracking reactions, injecting at least one HDD (hydrogen donor diluent) into the cracked product stream at or downstream of the point at which the reaction is quenched, recovering normally gaseous olefins from the cracked product stream, and recovering a liquid product stream containing a diminished asphaltene content.

Abstract: A two-step process for the production of large quantities of heartcut distillate resin precursors from steamed cracked gas oil product which involves hydrogenation of the steam cracked gas oil followed by steam cracking of the hydrogenated product to produce a greater than 15 wt. % yield of heartcut distillate resin precursors. A process for producing heartcut distillate comprising hydrogenating a hydrocarbon oil comprising two-ring aromatic molecules to form a hydrogenated hydrocarbon oil comprising partially saturated naphtheno-aromatic molecules; and subjecting a feedstock comprising hydrogenated hydrocarbon oil to steam cracking under conditions which favor producing a heartcut distillate containing an amount greater than about 4 wt. % yield of heartcut distillate resin precursors.A method for producing heartcut distillate which involves subjecting a hydrogenated hydrocarbon feedstock boiling in the range of about 200.degree. C. to 320.degree. C.

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: A process for catalytically cracking a hydrocarbon with simultaneous production of a low BTU fuel gas and catalyst regeneration comprising contacting a hydrocarbon feed, at elevated temperature and in a cracking zone, with a solid acid catalyst comprising a catalytic metal oxide component wherein said metal is selected from the group consisting essentially of (a) tungsten, niobium and mixtures thereof (b) mixture of (a) with tantalum, hafnium, chromium, titanium, zirconium and mixtures thereof, said oxide component being supported on a silica-containing inorganic refractory metal oxide support having a silica content less than 50 wt. % of the total support, to produce a cracked product and a deactivated catalyst and regenerating the deactive catalyst to produce a low BTU gas rich in CO, a gas rich in H.sub.2, or both and recirculating the regenerated catalyst back to the cracking zone, said catalyst being steamed prior to use at a temperature at least 600.degree. C.

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: A process is described for the catalytic cracking of a hydrocarbon feedstream involving the use of 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 supports, wherein (1) the feedstream is catalytically cracked by being contacted with said catalyst at a temperature and for a time (optionally, in combination with H.sub.2 O), sufficient to crack the hydrocarbon yielding a cracked product and a deactivated catalyst and (2) subjecting the deactivated catalyst to gasification conditions consisting of (A) partial oxidative combustion to produce a low BTU gas rich in CO or, (B) the addition of steam to produce a gas rich in H.sub.2, or both, with the recirculation of the decoked catalyst back to the first step.

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: 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.