Abstract: A multistage hydrocracking or hydrotreating process wherein a two-phase reaction mixture of a hydrogen rich gas stream and liquid hydrocarbon is passed through a series of spaced catalyst beds and reaction vapors are withdrawn at each interspace between beds and replaced with hydrogen. Such withdrawal and replacement reduces the partial pressure of NH.sub.3 and/or H.sub.2 S in the reaction mixture entering the bed succeeding each interspace, thereby increasing the reaction rate between hydrogen and the liquid hydrocarbon.

Abstract: An integrated hydrocarbon conversion process wherein two different heavy oil feed streams are thermally processed is disclosed. Preferably a vacuum gas oil is charged to a thermal cracking zone and a reduced crude fraction is charged to a visbreaking heater. The effluent of each thermal operation is separated into vapor and liquid fractions, with the vapor fractions being fed to a product fractionator. The liquid fractions each enter separate but interconnected subatmospheric pressure separation zones, one of which is a vacuum column. The bottoms of a product fractionator and distillate from the vacuum column are also charged to the thermal cracking zone.

Abstract: A method for maintaining a desired catalyst regeneration temperature in a fluid catalytic cracking unit operating with complete combustion of coke to carbon dioxide when the coke content of the spent catalyst supplied to the regeneration zone from the reaction zone is insufficient to maintain the temperature in the regeneration zone necessary for complete combustion of coke to carbon dioxide in which residual liquid hydrocarbon from the cracking reaction zone is introduced into contact with partially spent cracking catalyst at cracking reaction temperature effecting conversion of said residue to volatile reaction products and additional coke deposit on the spent catalyst in an amount sufficient to maintain the temperature in the regeneration zone necessary for complete combustion of coke to carbon dioxide and substantially complete removal of carbon from the catalyst.

Abstract: A process for upgrading oils is disclosed, in which the oil to be upgraded is contacted with liquid phase water and free oxygen at an elevated temperature and at a pressure sufficient to maintain at least part of the water in the liquid phase.

Abstract: In a process for cracking a sulfur-containing hydrocarbon an improved oxidation promoter for converting SO.sub.2 to SO.sub.3 comprising an intimate association of palladium and at least one other metal selected from the group comprising platinum, osmium, iridium, rhenium, and rhodium.

Abstract: There is provided a process for reduction of the nitrogen content of shale oil. The process comprises contacting shale oil with a low acid strength solvent in a first extraction zone, followed by contacting the shale oil with a high acid strength solvent in a second extraction zone. A portion of the high acid strength solvent containing extracted nitrogen-containing and non-nitrogen-containing compounds is passed to the first extraction zone and diluted to form low acid strength solvent, and at least a portion of the non-nitrogen-containing compounds redissolve into the shale oil in contact with the low acid strength solvent and are recovered. Thus, oil recovery is maximized at high nitrogen removal.

Abstract: An improved process for hydrocracking petroleum residuals wherein total conversion and the yield of lower boiling range products are increased. The hydrocracking is accomplished in the presence of a hydrogen donor solvent comprising substantially all of the liquid product having an initial boiling point substantially equal to the final boiling point of the liquid product recovered from the hydrocracked product and, generally, within the range from about 600.degree. F. to about 750.degree. F. and molecular hydrogen. The conversion is accomplished at a pressure within the range from about 1500 to about 2500 psig and at a temperature within the range from about 800.degree. to about 880.degree. F. Operation at these conditions is essential to achieving the increased conversion and the increased yield of lower boiling liquid products.

Abstract: Hydrocarbon process equipment is protected against fouling during processing of high sulfur-containing hydrocarbon feedstocks by incorporating into the hydrocarbon being processed small amounts of a composition comprised of an alkyl ester of a phosphorus acid and a hydrocarbon sulfonic acid.

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: A hydrocarbon material is subjected to mild hydrotreatment, washed, subjected to severe hydrotreatment and washed with only enough water to absorb all of the H.sub.2 S but only a fraction of the NH.sub.3 present in the hydrocarbon material. The effluent streams from each step of this process are segregated so that each may be fed separately to the optimum section of the recovery process. The washed hydrotreated hydrocarbon material is separated from the second effluent stream, and then a vapor phase is separated from the hydrocarbon material in a high pressure separator. The vapor phase is scrubbed with water to form an aqueous solution of NH.sub.3 with only a minor amount of H.sub.2 S (an NH.sub.3 to H.sub.2 S ratio of at least 6:1).

Abstract: A method of hydrocracking using a zinc catalyst in the hydrogenation step comprising providing a hydrocarbonaceous feed of coal or tar to a hydrogenation means,removing spent zinc and catalyst from said hydrogenation means to a regeneration means,heating said spent zinc catalyst in said regeneration means,providing hydrogen chloride to said regeneration means,said spent zinc catalyst comprising ZnS, whereby ZnCl.sub.2 gas is formed,contacting at least a portion of said ZnCl.sub.2 with steam to form ZnO,conveying said ZnO and ZnCL.sub.2 to said hydrogenation means.

Abstract: The present invention relates to a method for removing contaminants such as arsenic from a hydrocarbonaceous fluid which consists essentially of the crude, or a fraction thereof, obtained from oil shale, solid coal, or tar sands by non-catalytically heat treating the hydrocarbonaceous fluid at a temperature of from about 20.degree. F. to about 600.degree. F. in the presence of an aqueous solution containing an agent that would convert such contaminants into components soluble in the aqueous solution. Particularly suitable agents to be utilized in the above aqueous solution to remove contaminants such as arsenic are ammonium sulfide type compounds. The purified hydrocarbonaceous fluid may be subjected to a catalytic hydrotreating process.

Abstract: Hydrogen partial pressure in the distilled vapor phase in a stripper is maintained sufficienty to allow a smooth distillation processing whereby an efficient crude oil stripping is performed. The distillate overhead thus produced is maintained at a temperature high enough for direct feeding to a subsequent hydrotreating process by means of a reflux cooler installed at the top of the stripper.

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: Polymer precursor materials are vaporized without polymerization or are removed from a raw naphtha fraction by passing the raw naphtha to a vaporization zone (24) and vaporizing the naphtha in the presence of a wash oil while stripping with hot hydrogen to prevent polymer deposits in the equipment.

Abstract: Resids are hydrocracked at low pressure (600 psig and 825.degree. F.) in a solvent, while being demetalated, desulfurized, and decarbonized, by passing the solution through a dual-bed catalytic system having a large-pore catalyst as the first bed and a small-pore as the second bed. The solvent is preferably process generated and recycled, boiling at about 400.degree.-700.degree. F.

Abstract: Waxy, normal paraffin-type hydrocarbons present in petroleum oil feedstocks are selectively hydrocracked to hydrocarbons boiling below the boiling range of the feedstock by contacting the oil, in the presence of hydrogen, with a catalyst comprising a hydrogen form Zeolite L crystalline alumino-silicate containing at least one catalytic metal component selected from Group VIII and/or Group VI of the Periodic Table. This process is useful for dehazing oils such as white oils, for decreasing the pour point of jet fuels, for dewaxing lube oil feedstocks, including transformer oils and simultaneously reduces the aromatics content of the oil.

Abstract: The concentration of sulfur trioxides in an FCC unit regenerator is maintained within environmentally accepted limits, while maintaining an adequate amount of gas for fluidizing conditions in the regenerator, by admixing the regenerator oxygen-containing gas with an inert gas. The quantity of the inert gas is controlled by a control loop measuring the pressure drop in the regenerator, and adjusting the amount of the inert gas to maintain the pressure drop within the predetermined limits.

Abstract: The method of converting at least 20% by weight of a vacuum gas oil fraction boiling above 650.degree. F. into products having a boiling point less than about 650.degree. F., which comprises hydrotreating a vacuum gas oil with a hydrodesulfurization catalyst comprising a Group VIB and Group VIII metal wherein an organic fluorine compound is added to the vacuum gas oil during hydrotreating and the vacuum gas oil is hydrotreated under hydrogen at a temperature of at least 740.degree. F.

Abstract: Basic asphaltenes are selectively removed from asphaltene-containing hydrocarbon feeds by contacting the feed with a solid acid, such as a solid acid cracking catalyst, which selectively adsorbs the basic asphaltenes present in the feed. The adsorption is carried out at a temperature below about 575.degree. F. to avoid cracking the asphaltenes in the adsorption zone. The basic asphaltene-containing catalyst is then separated from the feed, the basic asphaltenes are cracked off the catalyst, the catalyst is regenerated by suitable techniques such as air burning and then recycled back to the adsorption zone. The basic asphaltene-reduced feed is sent to further processing.