Abstract: A process for producing a lubricating base oil having high oxidation stability, wherein the feed used to prepare the lubricating base oil contains at least 5 wt. % olefins, said process comprising (a) determining the weight percent of olefins present in the feed by means of 1H NMR; (b) hydroprocessing the feed under hydroprocessing conditions selected to reduce the amount of olefins present to a target value which has been pre-determined by means of 1H NMR to produce a lubricating base oil having the desired oxidation stability; and (c) collecting a lubricating base oil having the selected oxidation stability from the hydroprocessing zone.

Abstract: A process for steam cracking liquid hydrocarbon feedstocks containing synthetic crude oil comprises i) hydroprocessing a wide boiling range aliquot containing a) normally liquid hydrocarbon portion substantially free of resids and b) thermally cracked hydrocarbon liquid, boiling in a range from about 600° to about 1050° F., to provide a synthetic crude oil substantially free of resids; ii) adding to the synthetic crude oil a normally liquid hydrocarbon component boiling in a range from about 100° to about 1050° F.; and iii) cracking the mixture resulting from ii) in a cracker furnace comprising a radiant coil outlet to provide a cracked effluent, wherein the cracking is carried out under conditions sufficient to effect a radiant coil outlet temperature which is greater than the optimum radiant coil outlet temperature for cracking the synthetic crude oil separately. A method for upgrading synthetic crude for use in cracking is also provided, as well as a feedstock for cracking.

Abstract: Tar is contacted with stripping agent, such as steam or tail gas, in a stripping tower. A product comprising deasphalted tar is recovered as overheads and a product comprising heavy tar is recovered as bottoms from the stripping tower.

Abstract: A method of converting heavy oil into one or more valuable products comprises hydroconverting heavy oil, recovering an effluent stream from the hydroconverting, and deep catalytic cracking the effluent stream. The hydroconverting comprises reacting a slurry comprising unsupported fine catalyst in heavy oil. The effluent stream comprises unsupported fine catalyst in unconverted heavy oil. The deep catalytic cracking converts unconverted heavy oil into one or more light oil products.

Abstract: Less conventional sources of hydrocarbon feedstocks such as oil sands, tar sands and shale oils are being exploited. These feedstocks generate a larger amount of heavy oil, gas oil, asphaltene products and the like containing multiple fused aromatic ring compounds. These multiple fused aromatic ring compounds can be converted into feed for a hydrocarbon cracker by first hydrogenating at least one ring in the compounds and subjecting the resulting compound to a ring opening and cleavage reaction. The resulting product comprises lower paraffins suitable for feed to a cracker, higher paraffins suitable for example as a gasoline fraction and mono aromatic ring compounds (e.g. BTX) that may be further treated.

Abstract: The instant invention is directed to a new residuum full hydroconversion slurry reactor system that allows the catalyst, unconverted oil and converted oil to circulate in a continuous mixture throughout an entire reactor with no confinement of the mixture. The mixture is partially separated in between the reactors to remove only the products and hydrogen, while permitting the unconverted oil and the slurry catalyst to continue on into the next sequential reactor where a portion of the unconverted oil is converted to lower boiling point hydrocarbons, once again creating a mixture of unconverted oil, converted oil, and slurry catalyst. Further hydroprocessing may occur in additional reactors, fully converting the oil. The oil may alternately be partially converted, leaving a highly concentrated catalyst in unconverted oil which can be recycled directly to the first reactor.

Abstract: A new residuum full hydroconversion slurry reactor system has been developed that allows the catalyst, unconverted oil, products and hydrogen to circulate in a continuous mixture throughout an entire reactor with no confinement of the mixture. The mixture is partially separated in between the reactors to remove only the products and hydrogen while permitting the unconverted oil and the slurry catalyst to continue on into the next sequential reactor. In the next reactor, a portion of the unconverted oil is converted to lower boiling point hydrocarbons, once again creating a mixture of unconverted oil, products, hydrogen and slurry catalyst. Further hydroprocessing may occur in additional reactors, fully converting the oil. The oil may alternately be partially converted, leaving a highly concentrated catalyst in unconverted oil which can be recycled directly to the first reactor. The slurry reactor system is, in this invention, preceded by an in-line pretreating step, such as hydrotreating or deasphalting.

Abstract: Applicants have developed a new residuum full hydroconversion slurry reactor system that allows the catalyst, unconverted oil, hydrogen, and converted oil to circulate in a continuous mixture throughout an entire reactor with no confinement of the mixture. The mixture is separated internally, within one of more of the reactors, to separate only the converted oil and hydrogen into a vapor product while permitting the unconverted oil and the slurry catalyst to continue on into the next sequential reactor as a liquid product. A portion of the unconverted oil is then converted to lower boiling point hydrocarbons in the next reactor, once again creating a mixture of unconverted oil, hydrogen, converted oil, and slurry catalyst. Further hydroprocessing may occur in additional reactors, fully converting the oil. The oil may alternately be partially converted, leaving a concentrated catalyst in unconverted oil which can be recycled directly to the first reactor.

Abstract: The present invention relates to the field of hydroprocessing, and more particularly relates to a process directed to fuels hydrocracking and distillate feed hydrofining. This process has at least two stages. A relatively unconverted hydrofined product may be removed prior to the second stage, providing flexibility. In another embodiment, fresh feed may be added prior to the second stage. In both embodiments, fuels production is maintained at a constant level.

Abstract: The invention relates to a process for the treatment of heavy petroleum feedstocks in order to produce a gas oil fraction having a sulphur content of less than 50 ppm and generally 10 ppm which comprises the following stages: a) mild hydrocracking in a catalyst fixed bed, b) separation of the hydrogen sulphide, of a distillate cut including a gas oil fraction and of a fraction which is heavier than the gas oil, c) hydrotreating, by contact with at least one catalyst, of at least a portion of the said distillate cut obtained in stage b) including the gas oil fraction, as a mixture with a feedstock resulting from a crude or refined renewable source, d) separation of a gas oil cut comprising less than 50 ppm of sulphur. Advantageously, the heavy fraction is sent for catalytic cracking. Preferably, the process is carried out with makeup hydrogen introduced in stage c) and very advantageously all the makeup hydrogen for the process is introduced in stage c).

Abstract: A process to prepare a sweet crude from an ash containing and heavy fraction of a tar sand oil by: (a) supplying an atmospheric distillation bottoms of a tar sands originated feed to a vacuum distillation to obtain a vacuum gas oil and a vacuum bottoms, (b) contacting the vacuum gas oil with hydrogen in the presence of a suitable hydrocracking catalyst to obtain a sweet synthetic crude (c) separating the vacuum bottoms obtained in step (a) into an asphalt fraction comprising between 0.

Abstract: A process for conversion of a hydrocarbon feedstock comprising a relatively heavy main feedstock with a boiling point above approximately 350° C., and a relatively light secondary feedstock with a boiling point below approximately 320° C., wherein, the main feedstock, representing at least 50 wt. % of the hydrocarbon feedstock, is cracked in a fluidized-bed reactor in the presence of a cracking catalyst, the secondary feedstock is cracked in a fluidized bed with the same cracking catalyst, separately or mixed with the main feedstock, said secondary feedstock comprising oligomers with at least 8 carbon atoms of light olefins with 4 and/or 5 carbon atoms.

Abstract: A catalytic hydrocracking process for the production of ultra low sulfur diesel wherein a hydrocarbonaceous feedstock is hydrocracked at elevated temperature and pressure to obtain conversion to diesel boiling range hydrocarbons. The resulting hydrocracking zone effluent is hydrogen stripped in a stripping zone maintained at essentially the same pressure as the hydrocracking zone to produce a first gaseous hydrocarbonaceous stream and a first liquid hydrocarbonaceous stream. The first gaseous hydrocarbonaceous stream containing diesel boiling range hydrocarbons is introduced into a desulfurization zone and subsequently partially condensed to produce a hydrogen-rich gaseous stream and a second liquid hydrocarbonaceous stream containing diesel boiling range hydrocarbons. At least a portion of the first liquid stream is thermal cracked to produce diesel boiling range hydrocarbons. An ultra low sulfur diesel product stream is recovered.

Abstract: An integrated hydrocarbon conversion process for the production of low sulfur fuels utilizing a hydrocracking zone, a diesel hydrodesulfurization zone, a fluid catalytic cracking zone and a gasoline hydrodesulfurization zone. The hydrocracking zone is used to convert at least a portion of the feedstock into diesel boiling range hydrocarbons which are desulfurized in the first hydrodesulfurization zone. The unconverted feedstock is introduced into a fluid catalytic cracking zone to produce gasoline boiling range hydrocarbons which are desulfurized in a second hydrodesulfurization zone.

Abstract: The invention relates to the field of petrochemistry, in particular to a method of compressing a gaseous hydrocarbon-containing medium, for example, different hydrocarbon gases including flares produced in the oil refining and petrochemical industries. A distillate of a rectifying column of an atmosphere-vacuum oil refining unit is fed as the fresh liquid working medium into a circulation loop of a liquid hydrocarbon-containing medium, which contains a liquid-gas jet device, a separator and a pump. The liquid hydrocarbon-containing medium is removed from the circulation loop to a cracking and rectifying unit in which the liquid hydrocarbon-containing medium is subjected to cracking with subsequent rectification in the rectifying column of that unit.

Abstract: A VGO stream is initially hydrocracked in a hydrocracking reaction zone within an integrated hydroconversion process. Effluent from the hydrocracking reaction zone is combined with a light aromatic-containing feed stream, and the blended stream hydrotreated in a hydrotreating reaction zone. Heat exchange occurs between the hydrocracking reaction zone and the hydrotreating reaction zone, permitting the temperature control of the initial hydrocracking zone. The integrated reaction system provides a single hydrogen supply and recirculation system for use in two reaction processes.

Abstract: A process for treating a vacuum gas oil and Diesel feed includes the steps of providing reaction feed containing vacuum gas oil, Diesel and sulfur-containing compounds; providing a stripping gas; providing a washing feed; and mixing the reaction feed, the stripping gas and the washing feed in a stripping and washing zone so as to obtain a gas phase containing the sulfur-containing compounds and a liquid phase substantially free of the sulfur-containing compounds. The washing feed comprises at least one of Diesel, light vacuum gas oil and mixtures thereof produced in the process or added from external source.

Abstract: An integrated distillate hydrocracking process produces one or more fuel products and one or more lube products from a first reaction stage. Heavy fractions from the first stage, which are not recovered as lube products, are cracked to fuels in a second reaction stage. This invention is intended to provide a full range of lube streams, over a wide viscosity range and a wide viscosity index range, from a fuels hydrocracker, in addition to high yields of high quality fuels.

Abstract: A method for producing a lube basestock from a waxy feed is disclosed in which a feed containing to 50 wt % or more of wax is hydrotreated and stripped to lower the nitrogen and sulfur content of the feed. The feed is then hydroisomerized under conditions to 370° C. hydrocatalytically dewaxed with a catalyst comprising a mixture of a catalytically active metal on a zeolite dewaxing catalyst and an amorphous catalyst, or alternatively is solvent dewaxed and then hydrocatalytically dewaxed with the just described catalyst.

Abstract: For converting hydrocarbons: step a) treating a hydrocarbon feed with hydrogen in at least one three-phase reactor (1), containing ebullated bed hydroconversion catalyst; a step b) passing effluent from step a) to a separation zone (2) to recover a fraction F1 containing at least a portion of gas, gasoline and atmospheric gas oil contained in the effluent from step a), and a fraction F2 containing compounds with boiling points of more than that of the atmospheric gas oil; step c) hydrodesulphurizing at least a portion of fraction F1; and step d) passing at least a portion of fraction F2 to catalytic cracking section (6).

Abstract: The invention relates to a process for treating heavy petroleum feedstocks for producing a gas oil fraction that has a sulfur content of less than 50 ppm and most often 10 ppm that includes the following stages: a) ebulliated-bed catalytic hydrocracking, b) separation from hydrogen sulfide of a distillate fraction that includes a gas oil fraction and a heavier fraction than the gas oil, c) hydrotreatment of said distillate fraction, and d) separation of a gas oil fraction with less than 50 ppm of sulfur. Make-up hydrogen, preferably all make-up hydrogen, is to stage c). Advantageously, the heavier fraction from step (b) is subjected to catalytic cracking. The invention also relates to an installation that can be used for implementing this process.

Abstract: The invention relates to a process and installation for treating heavy petroleum feedstocks for producing a gas oil fraction that has a sulfur content of less than 50 ppm and most often 10 ppm that includes the following stages: a) mild hydrocracking in a fixed catalyst bed, b) separation from hydrogen sulfide of a distillate fraction that includes a gas oil fraction and a heavier fraction than the gas oil, c) hydrotreatment (including desulfurization) of said distillate fraction, and d) separation of a gas oil fraction with less than 50 ppm of sulfur. Advantageously, the heavy fraction is sent into catalytic cracking. The process preferably operates with make-up hydrogen that is brought to stage c), and very advantageously all of the make-up hydrogen of the process in introduced in stage c).

Abstract: A process for increasing the hydrogenation activity, particularly the carbon monoxide hydrogenation activity, of a catalyst or catalyst precursor comprised of a particulate solids support component and a catalytic metal, or metals component, preferably cobalt; cobalt alone or cobalt and an additional metal, or metals added to promote or modify the reaction produced by the cobalt. Treatment of the catalyst, or catalyst precursor is conducted at low temperature ranging from ambient to about 275° C. sufficient to form on the surface of a catalyst precursor, e.g., a cobalt catalyst precursor, a cobalt metal hydroxide, low valence cobalt metal oxide, or mixture of cobalt metal hydroxide and low valence cobalt metal oxide. Sometimes also metallic metal, e.g., cobalt, is also formed, and dispersed on the surface of the support.

Abstract: The invention relates to a process for the production of gasoline with a low sulfur content that comprises at least one stage for transformation of sulfur-containing compounds consisting of an alkylation or adsorption of sulfur-containing compounds and/or an increasing of the weight of light sulfur-containing compounds, at least one stage for treatment in the presence of an acid catalyst and at least one desulfurization treatment of at least a portion of the gasoline. The process according to the invention can also optionally comprise at least one stage for selective hydrogenation of diolefins and optionally at least one fractionation of the gasoline that is obtained into at least two fractions: light gasoline and heavy gasoline. FIG. 1 to be published.

Abstract: An aqueous low temperature oxidation (ALTO) process wherein a catalyst or catalyst precursor constituted of a solids support, or powder component, and a metal, or metals component, inclusive of cobalt, is oxidized, reduced and rendered catalytically active for conducting carbon monoxide hydrogenation reactions. The cobalt catalyst or cobalt catalyst precursor is thus contacted at low temperature with an oxidant in the presence of water (e.g., water to which an oxidant is added), sufficient to oxidize the cobalt metal, or metals component of the catalyst or catalyst precursor. On reduction, the hydrogenation activity of the cobalt catalyst is increased. All or a portion of the cobalt metal of the catalyst precursor is oxidized to form a Co2+ cationic or oxo-anionic species at least during the initial phase of the reaction.

Abstract: An integrated process for treating a vacuum gas oil, kerosene, naphtha and Diesel-containing feed, includes the steps of providing a reaction feed containing residue, vacuum gas oil, kerosene, naphtha, Diesel, hydrogen sulfide, ammonia, and C1-C4 gas phase compounds; providing a stripping gas; providing a washing feed; and feeding the reaction feed, the stripping gas and the washing feed to a stripping and washing zone so as to obtain a gas phase containing the hydrogen sulfide, the ammonia, the C1-C4 gas phase compounds, the naphtha, the kerosene, the Diesel and the vacuum gas oil and a liquid phase, wherein the reaction feed is provided at a reaction feed pressure of between bout 700 psig and about 3500 psig, and wherein the stripping and washing zone is operated at a pressure within about 80 psig of the reaction feed pressure.

Abstract: Low sulfur gasoline of relatively high octane number is produced from a catalytically or thermally cracked, olefin-rich, sulfur-containing hydrocarbon stream by hydrodesulfurization followed by treatment over an acidic catalyst containing a molecular sieve belonging to the MCM-22 family in combination with a metal component, preferably selected from the transition elements of the 4th and 5th periods of the Periodic Table. The treatment over the acidic catalyst in the second step restores the octane loss which takes place as a result of the hydrogenative treatment and results in a low sulfur gasoline product with an octane number comparable to that of the hydrocarbon feed.

Abstract: A catalytic hydrocracking process wherein a first hydrocarbonaceous feedstock is contacted with a hydrogen and a metal promoted hydrocracking catalyst in a hydrocracking reaction zone at elevated temperature and pressure to obtain conversion to lower boiling hydrocarbons. The resulting hot, uncooled effluent from the hydrocracking reaction zone is hot hydrogen stripped in a stripping zone maintained at essentially the same pressure as the hydrocracking zone to produce a first gaseous hydrocarbonaceous stream and a first liquid hydrocarbonaceous stream. At least a portion of the first liquid hydrocarbonaceous stream is preferably recycled to the hydrocracking reaction zone. A second hydrocarbonaceous feedstock having a boiling temperature range lower than that of the first hydrocarbonaceous feedstock is introduced into an upper end of the stripper to serve as reflux.

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: 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 at a pressure in the range of from about 400 psig to about 1,250 psig to effect substantially complete decomposition of organic sulfur and/or nitrogen compounds. The product from the hydrotreating zone is passed to a steam cracking zone. Hydrogen and C1-C4 hydrocarbons, steam cracked naphtha, steam cracked gas oil and steam cracked tar are recovered, where the amount of steam cracked tar produced is reduced by at least about 15 percent, basis the starting hydrocarbon feedstock which has not been subject to hydrotreating.

Abstract: Upgrading of a hydrocarbon feed containing sulfur, metals, and asphaltenes involves applying the feed to a distillation column for producing a substantially asphaltene-free, and metal-free distillate fraction and a non-distilled fraction containing sulfur, asphaltenes, and metals. At least some of the substantially asphaltene-free, and metal-free distillate fraction is converted to a hydrogen donor diluent. The non-distilled fraction is processed in a solvent deasphalting unit for producing a deasphalted oil stream and an asphaltene stream. After a combined stream is formed from the hydrogen donor diluent and the deasphalted oil stream, the combined stream is thermally cracked forming a thermally cracked stream that is applied to the distillation column.

Abstract: A hydroprocessing process includes a cocurrent flow liquid reaction stage, a countercurrent flow liquid reaction stage and a vapor reaction stage in which feed components are catalytically hydroprocessed by reacting with hydrogen. Both liquid stages both produce a liquid and a vapor effluent, with the cocurrent stage liquid effluent the feed for the countercurrent stage and the countercurrent stage liquid effluent the hydroprocessed product liquid. Both liquid stage vapor effluents are combined and catalytically reacted with hydrogen in a vapor reaction stage, to form a hydroprocessed vapor. This vapor is cooled to condense and recover a portion of the hydroprocessed hydrocarbonaceous vapor components as additional product liquid. The uncondensed vapor is rich in hydrogen and is cleaned up if necessary, to remove contaminants, and then recycled back into the cocurrent stage as hydrogen-containing treat gas.

Abstract: A process for upgrading petroleum feedstocks boiling in the distillate plus range, which feedstocks, when cracked, result in unexpected high yields of olefins. The feedstock is hydroprocessed in at least one reaction zone countercurrent to the flow of a hydrogen-containing treat gas. The hydroprocessed feedstock is then subjected to thermal cracking in a steam cracker or to catalytic cracking in a fluid catalytic cracking process. The resulting product slate will contain an increase in olefins compared with the same feedstock, but processed in by a conventional co-current hydroprocessing process.

Abstract: A process is described for the hydroisomerization/hydrocracking of paraffinic streams to yield lube oils of viscosity index of at least 105 and pour point -6.degree. C. or less, whereby a paraffinic feed which is enriched in iso-paraffins is submitted to hydrogenation in a bed made up of HDM, HDT, HDI/HCC and HDF catalysts, the product oil is separated by distilling the light fractions eventually present and dewaxed to remove the non-reacted high melting point paraffins. Equally considered is a variation in the process whereby diesel oil of high cetane number is produced by recirculating the 370.degree. C.+ cut to the process feed.

Abstract: A process is provided for preparing high quality Group II and Group III lubricating base oils from a sulfur containing feedstock using mild hydrotreating followed by isomerization/dewaxing followed by hydrogenation over a sulfur resistant hydrogenation catalyst.

Abstract: A process for the simultaneous production of lubricating blending stocks by means of hydrocracking a hydrocarbon feedstock in a first hydrocracking zone to convert at least a portion of the heavy hydrocarbon feedstock to produce an effluent stream containing lube oil boiling range hydrocarbons. One portion of the effluent stream is directly removed from the first hydrocracking zone to produce high quality lube oil blending stocks. Another portion of the effluent stream from the first hydrocracking zone is directly introduced into a second hydrocracking zone without intermediate separation. The second hydrocracking zone is utilized to further crack the feed to produce motor fuel.

Abstract: The hydroconversion of heavy petroliferous stocks boiling mainly above 400.degree. F. is carried out in a distillation column reactor where concurrently a petroleum stream is fed into a feed zone; hydrogen is fed at a point below said feed zone; the petroleum stream is distilled and contacted in the presence of a cracking catalyst prepared in the form of a catalytic distillation structure at total pressure of less than about 300 psig and a hydrogen partial pressure in the range of 1.0 to less than 70 psia and a temperature in the range of 400 to 1000.degree. F. whereby a portion of the petroleum stream is cracked to lighter products boiling below the boiling point of the feed and products are distilled to remove a vaporous overhead stream comprising products mainly boiling below the boiling point of the feed and a liquid bottoms stream.

Abstract: A process for producing normally gaseous olefins from two different process units sharing common downstream quench and fractionation facilities, wherein one of the process units is a short contact time mechanically fluidized vaporization unit for processing petroleum residual feedstocks and the other is a conventional steam cracking unit.

Abstract: A process for upgrading petroleum feedstocks boiling in the distillate plus range, which feedstocks, when cracked, result in unexpected high yields of olefins. The feedstock is hydroprocessed in at least one reaction zone countercurrent to the flow of a hydrogen-containing treat gas. The hydroprocessed feedstock is then subjected to thermal cracking in a steam cracker or to catalytic cracking in a fluid catalytic cracking process. The resulting product slate will contain an increase in olefins compared with the same feedstock, but processed in by a conventional co-current hydroprocessing process.

Abstract: This invention is directed to an improved process scheme to process sour feed in the reaction section of the process unit, including isomerization dewaxing with zeolite beta. The instant invention employs countercurrent flow in the fixed bed of the MIDW(Mobil Isomerization Dewaxing) reactor (the reactor in which isomerization dewaxing occurs) with recycle gas being the gas stream in the MIDW bed. With this arrangement hydrodesulfurization(HDS) and MIDW occur in an integrated process.

Abstract: Hydrocarbonaceous feedstocks admixed with a flow-through catalyst and hydrogen are hydroprocessed in a hydroprocessing reactor containing a captive hydroprocessing catalyst. The flow-through catalyst is continually withdrawn with the hydroprocessed feed from the hydroprocessing reactor. The flow-through catalyst may be an FCC, hydrocracking, isomerization or ring-opening catalyst. In a preferred embodiment, the captive hydroprocessing catalyst contains Co, Ni and/or Mo on an alumina base and the flow-through catalyst is an FCC zeolitic catalyst which is withdrawn with the hydroprocessed feed from the hydroprocessing reactor and then sent to an FCC unit.

Abstract: The invention provides a method for controlling the relative proportion of products produced from a petroleum residuum by thermal coking. Coke yield promoting compounds are identified, and effective attenuating agents are specified. The method can mitigate a coke promoting effect induced by certain surfactants, antifoulants, or fugitive catalysts in thermal coking units. Mitigating the coke yield promoting effect of molybdenum, for example, in a thermal coker permits recovery of a greater proportion of distillate boiling range products.

Abstract: A method of refining crude oil by distillation and desulfurization for the preparation of petroleum products can reduce cost of apparatus and cost of operation and can be operated with better stability by simplified control of operation. In the method, a naphtha fraction is separated from crude oil by distillation, the residual fraction which remained after the naphtha fraction has been removed from the crude oil is hydrodesulfurized and the hydrodesulfurized fraction is separated into further fractions by distillation. A kerosene fraction and a gas oil fraction of high quality can be obtained and yields of intermediate fractions such as kerosene and gas oil can be increased by introducing a hydrotreating process, a high pressure separation process and a residue fluid catalytic cracking process in a sophisticated way for refining of the residual fraction remained after the naphtha fraction has been removed from the crude oil.

Abstract: This invention relates to a process for cracking waste polymers in a fluidized bed reactor to produce vaporous products comprising primary products which can be further processed, eg in a steam cracker to produce olefins, characterized in that the vaporous products are treated to generate a primary product substantially free of a high molecular weight tail having molecular weights >700 prior to further processing. The removal of the high molecular weight tail minimizes fouling and prolongs the lifetime of the reactors used for further processing.

Abstract: A bottoms fraction of fuels hydrocracking which boils above about 600.degree. F. and contains at least 10 wt. % aromatics is converted to a reduced aromatics lube/base stock product over a catalyst comprising a crystalline material which exhibits unusually large sorption capacity demonstrated by its benzene adsorption capacity of greater than about 15 grams benzene/100 grams anhydrous crystal at 50 torr and 25.degree. C. and a-hydrogenation-dehydrogenation functionality, preferably palladium, under high pressure conditions sufficient to reduce the aromatics content to about 10 wt. %. The bottoms fraction is dewaxed prior to high pressure hydroprocessing over a catalyst comprising HZSM-5 to reduce the pour point of the fraction to about 20.degree. F. Typically, the bottoms fraction is produced in a moderate pressure fuels hydrocracking process over a bifunctional amorphous catalyst.

Abstract: A method of hydrotreatment of heavy hydrocarbon oil in the presence of catalysts which comprises hydrodemetallizing and hydrocracking the heavy hydrocarbon oil successively and thereafter hydrodesulfurizing and hydrodenitrogenating the treated heavy hydrocarbon oil. The hydrocracking is carried out in the presence of a catalyst comprising at least one metal or metal compound of the group VIA or the group VIII of the Periodic Table supported on a carrier comprising 10 to 90 weight % of an iron-containing aluminosilicate and 90 to 10 weight % of an inorganic oxide. Other methods of treatment of heavy hydrocarbon oil comprise the hydrotreatment in conjunction with fluid catalytic cracking and/or thermal hydrocracking. The methods provide a naphtha fraction, a kerosene fraction and a gas oil fraction which can be obtained from the heavy hydrocarbon oil efficiently with high yield.

Abstract: A fluid catalytic cracking process for producing relatively low emissions fuels. The feedstock is relatively low in nitrogen and aromatics and high in hydrogen content and the catalyst is a rare-earth promoted amorphous silica-alumina catalyst. The feedstock can be characterized as having less than about 50 wppm nitrogen; greater than about 13 wt. % hydrogen; less than about 7.5 wt. % 2+ ring aromatic cores; and not more than about 15 wt. % aromatic cores overall.

Abstract: A fluid catalytic cracking process for producing relatively low emissions fuels, The feedstock is relatively low in nitrogen and aromatics and high in hydrogen content and the catalyst is an amorphous acidic catalytic material which is promoted with up to about 5000 wppm chromium. The feedstock can be characterized as having less than about 50 wppm nitrogen; greater than about 13 wt. % hydrogen; less than about 7.5 wt. % 2+ ring aromatic cores; and not more than about 15 wt. % aromatic cores overall.

Abstract: A fluid catalytic cracking process for producing relatively low emissions fuels. The feedstock is exceptionally low in nitrogen and aromatics and relatively high in hydrogen and a 345.degree. C.+ products fraction is recycled to the cracking zone. The catalyst is an amorphous silica-alumina or a zeolitic material which is iso-structural to faujasite. The feedstock can be characterized as having less than about 50 wppm nitrogen; greater than about 13 wt. % hydrogen; less than about 7.5 wt. % 2+ ring aromatic cores; and not more than about 15 wt. % aromatic cores overall.

Abstract: A fluid catalytic cracking process for producing relatively low emissions fuels. The feedstock is relatively low in nitrogen and aromatics and high in hydrogen content and the catalyst is an amorphous silica-alumina containing a separate surface silica phase. The feedstock can be characterized as having less than about 50 wppm nitrogen; greater than about 13 wt. % hydrogen; less than about 7.5 wt. % 2+ ring aromatic cores; and not more than about 15 wt. % aromatic cores overall.