Abstract: A process is disclosed for the removal of iron from hydrocarbonaceous feedstock comprising passing the feedstock over inert, fibrous material in the presence of sulfur to induce the deposition of iron sulfide on the fibrous material through autocatalytic homoepitaxy.

Abstract: A process for selectively producing middle distillate fuel products from paraffin waxes such as slack wax and Fischer-Tropsch wax by hydroisomerizing the wax to convert 60-95 weight percent per pass of the 700.degree. F..sup.+ fraction contained in said wax. The catalyst employed is a fluorided Group VIII metal-on-alumina catalyst where the fluoride within the catalyst is present predominately as aluminum fluoride hydroxide hydrate. The preferred Group VIII metal is platinum.

Abstract: This invention provides a method for extending the catalytic dewaxing cycle time of a refined waxy lube stock. The method, in its broadest aspect, requires the additional refining step of thermally treating the refined waxy stock or precursor thereof for about 0.1 to about 2.0 hours at elevated temperature and at a pressure of 0 to 3000 psig (pounds per square inch gauge), and recovering an upgraded waxy stock having a reduced content of trace compounds that contain metals, nitrogen, sulfur and oxygen.In a specific embodiment of this invention, a vacuum residuum is thermally treated at a temperature of about 700.degree. F. to 950.degree. F. prior to solvent deasphalting and solvent extraction, and the waxy bright stock so formed is catalytically dewaxed with extended cycle time.

Abstract: Lubricants of improved characteristics are produced by carrying out a solvent extraction to remove aromatic components after solvent or catalytic dewaxing. Aromatic extraction solvents such as phenol, furfural or N-methyl pyrrolidone may be used. The process is particularly useful with wax-derived lubricants produced by the hydroisomerization of a petroleum wax which has then been dewaxed.

Abstract: A process for upgrading topped crude oils and residual portions comprising material boiling above 552.degree. C. (1025.degree. F.) by the combination of partial demetallizing and decarbonizing of the residual oil before effecting zeolite catalytic cracking thereof is described in conjunction with a product separation process, a combined hydrocarbon gas product concentration section and the use of parallel arranged CO boilers to produce sulfur free flue gas and steam. Steam generated by the combination operation effectively reduces the energy requirement of the combustion process.

Abstract: An effective, economical catalytic cracking process is provided to produce quality gasoline and other hydrocarbons from whole crude oil. The catalytic cracking process is operable and particularly useful during maintenance or shutdown of associated pipestills, vacuum tower, and/or atmospheric tower.

Abstract: A process for producing a pumpable syncrude from a Fischer-Tropsch wax by fractionating the wax into relatively low boiling fraction containing oxygenate compounds and a relatively high boiling fraction which is substantially free of oxygenate compounds and thereafter isomerizing/hydrocracking the low boiling fraction in the presence of hydrogen and a fluorided Group VIII metal-on-alumina catalyst. The preferred Group VIII metal is platinum.The pumpable syncrude is thereafter fractionated to produce a low boiling fraction which is thereafter isomerized/hydrocracked in the presence of hydrogen and a fluorided Group VIII metal-on-alumina catalyst to produce upgraded middle distillate fuel products. The preferred catalyst for middle distillate production is a fluorided platinum-on-alumina catalyst where a major portion of the fluoride within the catalyst is present as aluminum fluoride hydroxide hydrate.

Abstract: Disclosed is a method for accelerating the exchange of hydrogen between a hydrogen donor and a petroleum resid to be subjected to cracking, visbreaking, or coking. Acceleration is effected by incorporating an aqueous solution of ammoniun sulfide into the mixture of donor and resid and subjecting the mixture to a period of heat-soaking at an elevated temperature.

Abstract: A process is disclosed for the working up of salvage oil, in which the salvage oil is subjected to an extraction under supercritical conditions. The halogen compounds contained in the produced extract are removed by catalytic hydrogenation. The extraction residue is eliminated by deposition or thermal treatment (gasification). In the case of a thermal treatment of the extraction residue, other residues can be simultaneously converted, so that the process is performed without yield of environmentally burdensome residues or by-products. Ethane in particular and/or propane is employed as solvent for the supercritical extraction.

Abstract: Prior to upgrading a viscous feed by visbreaking, at least a portion of the feed is treated to remove a heavy phase in specified amounts, whereby the severity of the visbreaking may be increased. The Shell Hot Filtration number of the visbreaking product is reduced by at least 75%, compared to visbreaking of untreated feed at some severity.

Abstract: An improved heat balanced hydrocarbon conversion process is disclosed of the type employing circulating solids between a riser reactor (contactor) and regenerator (combustor). The ratio of circulating solid to hydrocarbon feed (C/O or cat-oil ratio) is increased by: directly cooling a portion of hot freshly regenerated contact material; passing a portion of hot regenerated material into the steam stripper; cooling hot regenerated contact material and charging it to the riser downstream of charging uncooled hot regenerated material which charging hydrocarbon feed to the base of the riser along with lift gas or steam; or lifting hot regenerated contact material by a carbonizable lift gas into the riser before contacting it with hydrocarbon feed which is injected higher in the riser.

Abstract: The coking tendencies of heavy hydrocarbon feedstocks are reduced by treatment with a free radical removing catalyst such as a transition metal naphthenate, preferably at temperatures below 350.degree. C. The treated product has improved stability as such and may be treated in subsequent processing operations such as catalytic cracking and thermal cracking, including visbreaking and coking, with improved liquid yield and reduced coke production.

Abstract: A hydrocarbon containing feed stream, e.g., a heavy oil or residuum, is contacted under suitable reaction conditions with a carbon monoxide containing gas, so as to produce a hydrocarbon stream having a reduced level of metal impurities, especially nickel and vanadium compounds, and an increased API.sup.60 gravity, essentially in the absence of a catalyst or extractant.

Abstract: Arsenic impurities and, optionally, iron impurities are removed from a hydrocarbon-containing feed stream, preferably shale oil, by contacting it with an aqueous solution of a metal chlorate and an acid having a pKa of less than 3.

Abstract: Hydrocarbon feedstocks, especially those high in Ramsbottom carbon, are vaporized by contact with a relatively inactive coked cracking catalyst, separating the resulting intermediate into a high and low boiling fraction, and cracking the high boiling fraction in a fluid catalytic cracker containing active cracking catalyst.

Abstract: Arsenic impurities are removed from a hydrocarbon-containing feed stream, preferably shale oil, by contacting it with an aqueous solution of a polyacrylamide.

Abstract: A treatment of highly viscous and very dense oils at the oil field to effect their desalting, and resulting in the production of an easily transportable hydrocarbon mixture of reduced viscosity, comprising the steps of:(a) diluting the crude oil with a hydrocarbon cut obtained in step (d);(b) subjecting the effluent from step (a) to a desalting-dehydration treatment;(c) subjecting the effluent from step (b) to hydrovisbreaking; and(d) distilling the effluent from step (c), and recycling a hydrocarbon cut to step (a), the remaining part forming a synthetic crude oil of reduced viscosity.

Abstract: A combination operation for upgrading reduced crudes is described which particularly restricts the contact time between hydrocarbons, solid sorbent material and cracking catalyst particles whereby quenching of visbroken product vapors is eliminated, coke formation is substantially restricted and catalytic cracking of hot product vapors of visbreaking contributes to the catalytic cracking thereof in a time-temperature restricted atmosphere providing substantial yields of gasoline and gasoline precursors.

Abstract: Used oils, especially used lubricating oils which are normally considered waste and are discarded or burned, are reclaimed for reuse by a re-refining procedure involving the steps of:(a) heat soaking the used oil;(b) distilling the heat soaked oil;(c) passing the distillate through a guard bed of activated material;(d) hydrotreating the guard bed treated distillate under standard hydrotreating conditions.If the used oil to be re-refined contains a quantity of water and/or fuel fraction which the practioner considers sufficiently large to be detrimental, the used oil may be subjected to a dewatering/defueling step prior to being heat soaked.

Abstract: A substantially solids-free sample of an oil having substantially the same hydrocarbon distribution as a heavy oil contained in a subterranean reservoir is prepared by vacuum-topping a field sample of the oil or oil-containing material while cold-trapping volatiles, diluting the topped oil with a volatile oil solvent, mechanically separating the solution from entrained solids, vacuum-distilling the solvent from the dissolved oil and recombining the oil and the cold-trapped volatiles.

Abstract: Unsaturated hydrocarbons and mixtures in which the latter are present are treated with anion exchangers prior to hydrogenation and are then hydrogenated catalytically in a known manner. The treatment with anion exchangers is carried out at 0.degree.-120.degree. C. and at a space velocity of 0.1 to 10 l of hydrocarbons to be hydrogenated per l of exchanger, per hour. The process avoids other, energy-intensive pretreatments, for example distillation of the hydrocarbons to be hydrogenated, or washing, and can be carried out in simple equipment. A considerable prolongation of the catalyst operating time is achieved in the subsequent catalytic hydrogenation.

Abstract: A hydrocracking process is provided in which the heavy bottoms fraction recovered from the hydrocracked product is heat treated prior to being recycled to the hydrocracking zone. The resulting hydrocracked product has an increased amount of constituents boiling in the middle distillate range.

Abstract: A process for fluid catalytic cracking of a starting oil selected from the group consisting of a distillation residual oil, a solvent deasphalted oil derived therefrom and a hydrodesulfurized oil derived therefrom, which comprises withdrawing a part of catalyst particles circulating through a fluid catalytic cracking unit, sending the withdrawn catalyst particles by means of a carrier fluid selected from the group consisting of air, nitrogen, steam and the mixtures thereof at a rate of 0.01 to 100 meters/second in a particle concentration of 0.

Abstract: A hydrocarbon feedstock containing organo-sulfur compounds, such as a naphtha containing mercaptans, is desulfurized by contact, under non-hydrogenative conditions, with a reduced catalytic absorbent comprising one or more nickel components and one or more platinum group metal promoters composited with a porous refractory oxide.

Abstract: Demetallized hydrocarbon feedstock is obtained from heavy oils by first solvent extracting the heavy oils and then demetallizing the extract in a magneto-filtration step. In another embodiment, diamagnetic nickel complexes in hydrocarbon oils are first converted to a paramagnetic product and the oil stream thereafter is passed through a magneto-filtration operation.

Abstract: An improvement in the solvent extraction of nonhydrocarbons from a synfuel liquid, e.g., shale oil, involves that the extract from the extractor, rather than being recycled directly back to the extractor, is first hydrotreated. A further improvement involves that a portion of the hydrotreated extract is fractionated and a light fraction is returned to the extractor. Use of the hydrotreated extract as recycle increases the efficiency of the extractor. A still further improvement involves the use as a selective solvent of one of the following: dialkylformamide, aldehydomorpholine, keto-morpholine, morpholine or an aliphatic aromatic ketone. These preferred solvents have the advantage of providing a clear interface between the extract and raffinate in the extractor. Removal of the nonhydrocarbons permits production of more hydrocarbons having enhanced utility as a jet fuel from a synfuel liquid than otherwise would be possible.

Abstract: A process is provided for the production of an aciculate textured coke from pitch comprising the steps of filtering at least two different bituminous coal tar pitches having differing softening points at an elevated temperature to form a mixture of the filtrate having a viscosity of 50-200 centipoise at 250.degree.-260.degree. C. and producing an aciculate textured coke by coking said mixture.

Abstract: Manufacture of pitch coke with needle-like structure by mixing pyrolysis oil condensate formed in the process with a coal-tar pitch having a softening point between 70.degree. and 150.degree. C, filtering the mixture at a temperature 100.degree. to 200.degree. C above the softening point, heating the filtrate to a temperature between 450.degree. and 525.degree. C in a tubular heater and coking the heated filtrate in a coking drum, passing volatile pyrolysis products from the drum to a fractionating column for separation of pyrolysis oil condensate from non-condensible gas.

Abstract: Upgrading of 350.degree. F plus product of Fischer-Tropsch Synthesis is accomplished by hydrotreating the Fischer-Tropsch Synthesis product and selective cracking the hydrotreated material boiling above about 600.degree. F. A product slate is recovered comprising LPG, gasoline, jet fuel, light and heavy oil fractions.

Abstract: Upgrading a Fischer-Tropsch synthesis product by separating a 350.degree. to 850.degree. F product fraction thereof into a 650.degree. F minus fraction and a 650.degree. F plus fraction; separating the 650.degree. F minus fraction to provide a more narrow 350.degree. to 650.degree. F fraction; combining the 650.degree. F plus fraction with a portion of the 350.degree. to 650.degree. F fraction to form a wide boiling range feed material; contacting this formed wide boiling range feed material, together with hydrogen, with a special catalyst comprising a crystalline aluminosilicate zeolite having a silica to alumina ratio of at least 12 and a constraint index of 1 to 12, at a temperature of about 500.degree. to 800.degree. F, a hydrogen partial pressure of about 100 to 800 psia and a space velocity of about 0.5 to 5 LHSV to produce a converted product thereof separating the zeolite conversion product to recover a 350.degree. F minus fraction from a 350.degree. F plus fractions; and separating the 350.degree.

Abstract: A two-step process for preparing a stabilized lubricating oil resistant to oxidation and sludge formation upon exposure to a highly oxidative environment is provided. The first step of the present process comprises contacting a lubricating oil stock with elemental sulfur in the presence of a catalyst material selcted from the group consisting of alumina, silica, aluminosilicate, a metal of Groups II-A, II-B, VI-B or VIII of the Periodic Table of Elements, an oxide of a metal of Groups II-A, II-B, VI-B or VIII, a sulfide of a metal of Groups II-A, II-B, VI-B or VIII, clay, silica combined with an oxide of a metal of Groups II-A, III-A, IV-B or V-B, and combinations thereof in a flow reactor or under conditions comparable to those existing in a flow reactor. The second step of the present process comprises contacting the product of the first step with hydrogen in the presence of alumina impregnated with at least about 10 weight percent of MoO.sub.3 and at least about 2.

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

Abstract: A process for producing coke from sulfur-containing hydrocarbon feedstocks which involves contacting at least a portion of the feedstock with a peroxy oxidant in the presence of a metal-containing catalyst to preferentially oxidize a portion of the hydrocarbon feedstock, subjecting the feedstock to coking conditions to form coke and recovering a coke product. The present process can provide improved yields of coke having substantially reduced sulfur content.

Abstract: The products of Fischer-Tropsch synthesis boiling below a separated decant oil fraction are subjected to cooling to a temperature of about 100.degree. F and separation of the cooled product to recover Fischer-Tropsch produced water comprising oxygenates, a normally liquid hydrocarbon phase comprising absorbed oxygenates and a gaseous phase normally comprising a substantial amount of C.sub.5 hydrocarbons in combination with lower boiling materials including unreacted synthesis gas and carbon dioxide. Each of said gaseous phase and said normally liquid hydrocarbon phase are thereafter contacted with a selected crystalline zeolite catalyst particularly selective for the formation of gasoline boiling material of high octane.

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 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 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: 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: 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 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 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: 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.