Abstract: In a crude oil refining apparatus, heavy cycle oil from the catalytic cracking unit employed in the crude oil refining apparatus is recycled to a hydrofining process. Such recycling improves the value of the product mix obtained from the crude oil refining apparatus with respect to an apparatus in which the heavy cycle oil withdrawn from the catalytic cracking units is recycled to the catalytic cracking units.

Abstract: Temperature is controlled in a hydrogenation reactor without changing the flow rate of feed into the reactor to maintain a pre-determined temperature in the reactor. In one embodiment, the firing rate of a fuel fired furnace for heating feed to the reactor is controlled in response to the temperature sensed in the reactor to maintain a pre-determined temperature. In another embodiment, the flow rate of a quenching stream for cooling feed to the reactor is controlled in response to temperature sensed in the reactor to maintain a pre-determined temperature in the reactor.

Abstract: Full-range shale oils or fractions thereof, after hydrotreating, are hydrodewaxed and then hydrogenated to produce lubricating oil fractions boiling above 650.degree. F., having a pour point at or below +10.degree. F., and a viscosity index of at least 95.

Abstract: Low-molecular weight olefins from heavy hydrocarbons are obtained with a hydrogenating pretreatment and a subsequent thermal cracking of at least a portion of the hydrogenated product. In the first stage, the polyaromatic content of a first hydrocarbon fraction high in polyaromatic compounds, e.g., a vacuum gas oil, is selectively degraded with a zeolitic hydrotreating catalyst, and in a second stage the resultant hydrocarbons are refined with a non-zeolitic hydrotreating catalyst in admixture with a second heavy hydrocarbon fraction low in polyaromatic compounds, e.g., and atmospheric gas oil. This two-stage process permits the utilization of lower operating pressures as compared to the separate treatment of the heavy hydrocarbon fractions.

Abstract: A process for producing high quality, high molecular weight microcrystalline wax from a hydrocracked, undewaxed bright stock, comprising hydrodenitrification, mild hydrofinishing, and solvent dewaxing.

Abstract: The present invention is concerned with upgrading residual oils to gasoline product with a coke selective hydrogen stable faujasite crystalline zeolite catalyst comprising at least 40 weight percent of alumina and rare earth metals in an acidic matrix and effecting regeneration thereof in an oxygen lean atmosphere under CO combustion conditions. A compound of antimony is added to passivate metal contaminants. The regeneration of the catalyst is effected to retain up to 0.25 weight percent carbon and heat balance of the operation is limited as a function of metal promoted CO burn within a dense fluid bed of catalyst being regenerated.

Abstract: In a crude oil refining process, heavy cycle oil from the catalytic cracking unit employed in the crude oil refining process is recycled to a hydrofining process. Such recycling improves the value of the product mix obtained from the crude oil refining process with respect to a process in which the heavy cycle oil withdrawn from the catalytic cracking units is recycled to the catalytic cracking units.

Abstract: A hydrocarbonaceous feedstock upgrading process is disclosed. Spent nickel arsenide-containing catalyst from demetallation guard chambers or hydroprocessing operations are utilized to upgrade the hydrocarbonaceous feedstock prior to dearsenation. The spent catalysts have significant activity for diolefin saturation and CCR removal at temperatures low enough to reduce olefin polymerization reactions.

Abstract: A process is disclosed for converting a non-distillable residue of a mixed-base or paraffin-base crude hydrocarbon oil to a distillable precursor for motor fuels and/or petrochemical products which comprises donor solvent hydrovisbreaking said residue in a hydrovisbreaking zone in the presence of a circulated hydrogen donor solvent at a temperature in the range of 380.degree. to 480.degree. C.

Abstract: An improved process for upgrading vacuum resids to premium liquid products which comprises mild hydrotreating of the vacuum resids followed by fractionating and short contact time thermal cracking of the fraction boiling above 850.degree. F.+, such as by short contact time thermal cracking or rapid pyrolysis.

Abstract: Straight-chain hydrocarbons and slightly branched chain hydrocarbons are selectively converted utilizing highly siliceous porous crystalline materials of the zeolite type having SiO.sub.2 /Al.sub.2 O.sub.3 ratio of greater than 200, unique molecular sieving properties and superior resistance to ammonia deactivation. The catalyst preferably contains acidic cations and can also contain a component having a hydrogenation/dehydrogenation function. The process of this invention is particularly useful for the dewaxing of hydrocarbon oils, including removal of high freezing point paraffins from jet fuel to lower freezing point, as well as improving the octane rating of naphtha fractions.

Abstract: A process for upgrading a heavy hydrocarbonaceous oil is provided in which the oil is hydrorefined, heat-treated and hydrocracked to increase the selectivity of the hydrocracked product to components boiling in the range of 350.degree. to 675.degree. F.

Abstract: The invention relates to a process to improve the stability of a catalyst to be used for lowering the cloud or turbidity point and the filterability limit temperature of gas-oils.The catalyst is formed of a composite system constituting 5 to 90% of a hydrodesulfuration type catalyst A and 95 to 10% of a hydroconversion type catalyst B, these two catalysts being either mixed or superposed, in which case catalyst A forms the top of the catalytic bed.

Abstract: Heavy carbonaceous liquid having a melting point below 250.degree. C. is upgraded to lighter products by hydrogen donor solvent cracking, using recycled solvent derived at least in part from a middle distillate fraction of either the heavy carbonaceous liquid or from the cracked products which is subjected to one or more catalytic hydroprocessing steps before recycling.

Abstract: Improved method for maximizing jet fuel from shale oil involves hydrotreating the treated oil at a temperature of about 600.degree.-650.degree. F. in the presence of a catalyst having a relatively low metal content and then hydrotreating the oil at a temperature in excess of about 800.degree. F. in the presence of a catalyst having a relatively high metal content. A 480.degree. F. minus boiling point fraction fractionated from the foregoing process can meet JP-4 jet fuel specifications. Hydrocracking the 480.degree. F. plus boiling point fraction results in substantial additional quantities of jet fuel.

Abstract: For thermally cracking heavy liquid hydrocarbons to produce gaseous olefins comprising a catalytic hydrogenating pretreatment, a separation of the hydrogenation product into a lighter fraction and a heavier fraction; passing the heavier fraction at least in part to a thermal cracking step to produce normally gaseous olefins; and withdrawing the lighter fraction, the improvement wherein the hydrogenation is conducted within the shaded area of FIG. 2, whereby said lighter fraction has a higher octane number.

Abstract: To obtain olefins by the thermal cracking of hydrocarbons, e.g., vacuum gas oil, by hydrogenation and subsequent steam cracking, an intermediate fractionation of the hydrogenate is provided so that the light fraction enriched in branched isomers can be used as fuel and the heavy fraction only is subjected to the steam cracking.

Abstract: Hydrocarbons are subjected to hydrogenation, pressure reduction and separation into liquid and gaseous fractions. The gaseous fractions are purified and desulfurized. Hydrogen-rich components of the gaseous fraction are returned to the hydrogenation stage. Hydrocarbon-rich components of the gaseous fraction and components of the liquid fraction are cracked and fractionated. Residue is partially oxidized with oxygen and steam. Gas produced by the partial oxidation is desulfurized and separated, and hydrogen is returned to the hydrogenation stage. A polymer free fraction of the residue is returned to the feed stock and to the hydrogenation stage, a heavy residue component of the initial liquid fraction is partially oxidized with the residue.

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 method is disclosed for reducing the nitrogen content of shale oil using mild hydrogenation followed by liquid sulfur dioxide extraction of the hydrogenated shale oil. The mild hydrogenation is effective for increasing the fraction of shale oil that is insoluble in the liquid sulfur dioxide. The mild hydrogenation is sufficient for saturating unsaturated compounds present in the shale oil to the substantial exclusion of adding hydrogen to the nitrogen of the nitrogen-containing compounds. Following hydrogenation of the shale oil, it is extracted with liquid sulfur dioxide at a temperature from about 14.degree. F. to about 60.degree. F. forming two fractions, a liquid sulfur dioxide insoluble fraction containing a relatively low nitrogen content and a liquid sulfur dioxide soluble fraction containing a relatively high nitrogen content. The liquid sulfur dioxide fraction is separated from the insoluble shale oil fraction. The liquid sulfur dioxide can be recovered for recycling to another extraction step.

Abstract: The preparation of food grade white mineral oils of suitable viscosity in high yield from a mineral oil distillate of suitable lubricating oil viscosity comprises contacting the distillate with hydrogen in three catalytic stages to yield a refined lubricating oil from which white mineral oil is recovered. The first reaction stage employs hydrocracking conditions. Subsequent reaction stages employ hydrogenation conditions, first with a sulfur-resistant hydrogenation catalyst and finally with a platinum group metal-containing selective hydrogenation catalyst, optionally activated with a halogen.

Abstract: To obtain olefins by the thermal cracking of hydrocarbons, e.g., vacuum gas oil, by hydrogenation and subsequent steam cracking, an intermediate fractionation of the hydrogenate is provided so that the light fraction enriched in branched isomers can be used as fuel and the heavy fraction only is subjected to the steam cracking.

Abstract: Hydrocarbon oils, especially waxy distillate lubricating oil stocks suitable for the preparation, by conventional unit processes, of high V.I., low pour point lubricating oils, are advantageously catalytically dewaxed with synthetic offretite catalyst preferably associated with a hydrogenation metal such as platinum or palladium.

Abstract: Vacuum residue is used for production of olefins by first separating, preferably by solvent extraction, the asphalt therein, blending resultant asphalt depleted fraction with a lighter fraction, e.g., a vacuum gas oil, and then subjecting the blend to a conventional catalytic hydrogenation step prior to thermal cracking. The hydrogenate may be separated into fractions with the heavy fraction only being thermally cracked.

Abstract: A process for preparing white mineral oil from a mineral oil distillate of lubricating viscosity by first contacting the distillate with hydrogen in the presence of sulfur-resistant catalyst to form hydrogenated oil and then second contacting at least a portion of the hydrogenated oil with hydrogen in the presence of a second catalyst to form a refined oil from which white oil is recovered. The second catalyst, which comprises a support, at least one palladium component and at least one halogen component, possess improved catalyst activity.

Abstract: A process which comprises fractionating a wide-boiling range naphtha feedstock into a low-boiling, light-naphtha fraction having an end or maximum boiling point within the range of about 190.degree. to about 200.degree. F. (88.degree. to about 104.degree. C.), and a high-boiling, heavy-naphtha fraction having an initial boiling point within a range of about 190.degree. to about 220.degree. F. (88.degree. to about 104.degree. C.), and contacting the light-naphtha fraction in an isomerization zone with added hydrogen and a catalyst comprising tantalum pentafluoride and hydrogen halide to produce effluent yielding naphthene components which are blended with the heavy-naphtha fraction. The resulting blended material can be processed by reforming to produce an aromatic-rich naphtha product and hydrogen.

Abstract: A process for the treatment of a hydrocarbon fraction having a boiling point range beginning above 200.degree. C. and obtained in the cracking of hydrocarbons, in which the polymeric component resulting from the cracking pyrolysis is removed and the remaining polymer-free hydrocarbon is subjected to hydrogenation under such reaction conditions that the product is high in monoaromatic components while the polyaromatics are removed therefrom.

Abstract: A two-stage naphtha hydrorefining process is provided with interstage removal of hydrogen sulfide and light gaseous hydrocarbons. Fresh hydrogen-containing treat gas is introduced only into the second hydrorefining stage and the hydrogen-containing gaseous effluent of the second hydrorefining stage is recycled to the first hydrorefining stage.

Abstract: In an olefin plant in which ethylene, propylene and butenes are prepared, a dripolene fraction is recovered, hydrogenated and a C.sub.6 -C.sub.7 hydrogenated hydrocarbon stream derived from such hydrogenated dripolene is aromatized in the presence of a hydrogen rich recycle stream and in the presence of a catalyst containing platinum and chloride on aluminum whereby the aromatics content is increased above the approximately 64% aromatics content of the hydrogenated C.sub.6 -C.sub.7 hydrocarbon stream. The aromatics are extracted from the liquid effluent from the aromatization zone.

Abstract: In a selective hydrogenation process wherein at least two catalyst beds in series are utilized, the temperature of the feed stream to the first catalyst bed and the temperature of the feed stream from the first catalyst bed to the second catalyst bed is controlled so as to maintain a desired reaction temperature in both catalyst beds and to maintain a desired relationship between the amount of the impurity selectively hydrogenated in the first catalyst bed and the amount of the impurity selectively hydrogenated in the second catalyst bed.

Abstract: A hydrocarbon feedstock derived from crude oil or other sources is subjected continuously to thermal cracking under pressure and in the presence of hydrogen in order to convert the feedstock to products of lower molecular weight containing high proportions of olefinic components. In a first processing step, a catalytic hydrogenating pretreatment is performed at a temperature within the range of 300.degree. C. to 600.degree. C. and under a pressure within the range of 12 to 85 bars. In a second step, a thermal cracking treatment is performed under a pressure within the range of 10 to 70 bars with residence times of less than 0.5 second and at a temperature within the range of 625.degree. C. to 1,000.degree. C., the quantity of hydrogen employed being such that the molar concentration in the effluents is at least equal to 20%.

Abstract: In a process for the production of olefins in two stages wherein, in the first stage, heavy petroleum fractions are hydrogenated in the presence of hydrogen and a hydrogenation catalyst and, in the second stage, the thus-hydrogenated fractions are subjected to thermal cracking in the presence of steam, the improvement which comprises employing as the hydrogenation catalyst a support-free catalyst consisting essentially of elements from Groups VIb, VIIB, and VIII of the periodic table of the elements in the form of the metals, metal oxides, metal sulfides, or organometal complexes, or mixtures thereof.

Abstract: A process for producing benzene is provided which comprises the steps of subjecting a charge rich in alkylaromatic hydrocarbons and containing 2-20% by weight paraffinic and/or naphthenic hydrocarbons, in a first catalytic zone, to a hydrotreatment in the presence of a catalyst mixture containing a selective mordenite catalyst and a reforming catalyst, then subjecting at least a portion of the resultant effluent to thermal or catalytic hydrodealkylation in a second zone, and separating and recovering benzene from the effluent from the second zone.

Abstract: In a process for the production of olefins in two stages wherein, in the first stage, heavy petroleum fractions are hydrogenated in the presence of hydrogen and a hydrogenation catalyst and, in the second stage, the thus-hydrogenated fractions are subjected to thermal cracking the presence of steam, the improvement which comprises employing as the hydrogenation catalyst a zeolite of the faujasite structure combined with elements from Groups VIB, VIIB and VIII of the periodic table of the elements, wherein the alkali component of the zeolite is exchanged at least partially for ammonium, hydronium, alkaline earth and/or rare earth ions, and the elements are present in a metallic, ionic, oxidic and/or sulfidic form.

Abstract: A pyrolysis feedstock, such as a gas oil feed, is hydrotreated in the presence of a bimetallic catalyst which has been promoted by the addition of chlorine and/or fluorine, preferably chlorine, followed by thermal cracking to increase the yields of light olefins and BTX.

Abstract: A fresh charge containing aromatic hydrocarbons is hydrotreated in admixture with a recycle fraction, in the presence of a bifunctional catalyst, a portion of the effluent is subjected to steam-cracking, thereby recovering a gas oil fraction which is subjected to hydrogenation and forms said recycle fraction. The mixture of recycle fraction and charge is advantageously treated with hydrogen in the presence of a monofunctional catalyst to hydrogenate olefins, at a lower temperature than the hydrotreatment, and then passed to the hydrotreatment zone.

Abstract: A catalytically hydrogenated naphtha stream containing less than 10 ppm by weight of sulfur is pyrolyzed without added hydrogen to a product including ethylene. Selectivity to ethylene is increased by adding a sulfur compound to increase the sulfur content to above 20 ppm by weight based on hydrogenated naphtha. Addition of the sulfur compound increases the quality of hydrogenated naphtha as a pyrolysis feedstock nearly to that of a C.sub.2 to C.sub.5 paraffin stream.

Abstract: A cycle oil is hydrogenated under conditions such that the product of the hydrogenation process can be fractionated to obtain a more valuable naphtha reforming charge stock and a furnace oil fraction.

Abstract: An unstable heavy hydrocarbon fraction obtained by pyrosis is reacted with hydrogen in contact with three successive catalysts:(a) a group VIII metal catalyst(b) a catalyst comprising nickel and tungsten compounds, and(c) a catalyst comprising alumina, a group VIII noble metal and fluorine or chlorine.

Abstract: Fischer-Tropsch synthol naptha is upgraded to high octane gasoline with minimum yield loss in a multistep process comprising fractionating the synthol naptha to give a C.sub.5 + C.sub.6 fraction and C.sub.7.sup.+ fraction, processing the C.sub.5 + C.sub.6 fraction over a ZSM-5 catalyst under dense phase conditions, pretreating and reforming the C.sub.7.sup.+ fraction under conventional conditions, and blending the C.sub.5.sup.+ products from both the C.sub.5 + C.sub.6 and C.sub.7.sup.+ processing steps.

Abstract: Hydrocarbon tars of high asphaltene content such as tars obtained from pyrolysis of coal are dissolved in a solvent formed from the hydrogenation of the coal tars, and the resultant mixture hydrogenated in the presence of a catalyst at a pressure from about 1500 to 5000 psig at a temperature from about 500.degree. F to about the critical temperature of the solvent to form a light hydrocarbon as a solvent for the tars. Hydrogen content is at least three times the amount of hydrogen consumed.

Abstract: A process for making naphthenic type lubricating oils from a low VI waxy crude which comprises distilling said low VI waxy crude to 500.degree. to 650.degree. F at atmospheric pressure to separate distillable fractions therefrom, subjecting the residue to a vacuum distillation at about 25 to about 125 mm Hg absolute pressure to obtain one or more gas oil fractions, optionally hydrotreating said gas oil fractions in the presence of a Ni/Mo catalyst at 550.degree. to 650.degree. F, 0.25 to 1.0 LHSV, and 700-1500 psig, and catalytically dewaxing said distillates in the presence of a H.sup.+ form mordenite catalyst containing a Group VI or Group VIII metal at 550.degree. to 750.degree. F, 500 to 1500 psig and 0.25 to 5.0 LHSV, to obtain said naphthenic type oils having pour points to from about -60.degree. to +20.degree. F.

Abstract: In a thermal cracking process employing inert hot solids as a heat source, the cracker effluent solids are passed to a burner for combustion of deposited and entrained coke. The liquid product of the thermal cracking process is distilled and the liquid residue comprises a low value solids-containing slurry which is used as a torch oil in the coke burner. The liquid residue from a catalytic cracking process also comprises a low value slurry since it contains particles of cracking catalyst and in the present process is used as auxiliary torch oil in the solids burner. The catalyst particles are rendered inert at the high temperature of the burner, thereby enhancing the quantity of inert solids circulating in the thermal cracking process. The use of a second slurry as torch oil reduces the quantity of thermally cracked liquid residue required as torch oil and enhances the quantity of more valuable solids-free distillate liquid recoverable from the thermal cracking process.

Abstract: The invention relates to an integrated process for the production of normally gaseous olefins, starting from a petroleum residue.

Abstract: A process for the production of ethylene by the non-catalytic riser cracking of hydrodesulfurized residual petroleum oils in the presence of entrained hot, inert solids.

Abstract: Upgrading a product of Fischer-Tropsch Synthesis boiling above 300.degree. F is accomplished in a combination operation comprising hydrotreating of the 300.degree. F plus product and selective cracking portions of the hydrotreated product to provide a product slate comprising gas, gasoline, jet fuel, light and heavy oil fractions.

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: Naphthenic solvents and low aromatics mineral spirits are produced simultaneously by blending a hydrocarbon oil boiling in the range between about 100.degree. F. and about 600.degree. F. with an aromatics fraction having an initial boiling point similar to that of the oil to produce a blend containing in excess of about 10 weight percent aromatics, hydrogenating the blend in the presence of a hydrogenation catalyst until aromatics present in the blend have been converted into lower boiling naphthenic compounds, and thereafter fractionating the hydrogenated material to produce a highly naphthenic overhead fraction useful as a solvent and a low aromatics bottom fraction useful as mineral spirits.

Abstract: Hydroprocessing a high boiling hydrocarbon feed, such as coker gas oil, containing an aromatic carbon content of at least 35%, thereby reducing the aromatic carbon content level to less than 35% but not less than about 20%, prior to inclusion of this FCC feed component with the remainder of the FCC feed or cracking it alone with a crystalline zeolite aluminosilicate in a catalytic cracking zone.

Abstract: A process for making naphthenic type lubricating oils from a low VI waxy crude which comprises distilling said low VI waxy crude to 500.degree. to 650.degree. F. at atmospheric pressure to separate distillable fractions therefrom, subjecting the residue to a vacuum distillation at about 25 to about 125 mm Hg absolute pressure to obtain one or more gas oil fractions, optionally hydrotreating said gas oil fractions in the presence of a Ni/Mo catalyst at 550.degree. to 650.degree. F., 0.25 to 1.0 LHSV, and 700-1500 psig, and catalytically dewaxing said distillates in the presence of a H.sup.+ form mordenite catalyst containing a Group VI or Group VIII metal at 550.degree. to 750.degree. F., 500 to 1500 psig and 0.25 to 5.0 LHSV, to obtain said naphthenic type oils having pour points of from about -60.degree. to +20.degree. F.