Abstract: A process for converting a hydrocarbon fraction comprises a step a) for treating a hydrocarbon feed in the presence of hydrogen in at least one three-phase reactor, containing at least one hydrotreatment catalyst in an ebullating bed, operating in riser mode of liquid and of gas, the reactor comprising at least one means located close to the bottom of the reactor for extracting catalyst from the reactor and at least one means located close to the top of the reactor for adding fresh catalyst to the reactor, a step b) for treating at least a portion of the effluent from step a) in the presence of hydrogen in at least one reactor containing at least one hydrocracking catalyst in a fixed bed under conditions for producing an effluent with a reduced sulphur content, and a step c) in which at least a portion of the product from step b) is sent to a distillation zone from which a gaseous fraction, a gasoline type engine fuel fraction, a diesel type engine fuel fraction and a liquid fraction which is heavier than the

Abstract: A process for converting a heavy hydrocarbon fraction comprises treating the hydrocarbon feed in a hydrodemetallization section, the section containing at least one fixed bed hydrodemetallization catalyst.

Abstract: A process for the reduction of sulphur content in a FCC gasoline includes fractionation of the FCC gasoline into three fractions: a light fraction comprising 50-80% of the FCC gasoline, an intermediate boiling fraction comprising 10-30% of the FCC gasoline, and a heavy fraction comprising 5-20% of the FCC gasoline. The heaviest fraction is hydrotreated in the first bed of a hydrotreater at conditions that result in essentially total removal of the sulphur. The effluent from the first bed is quenched with the intermediate fraction. The combined oil stream is hydrotreated in a second and final bed in the hydrotreater at conditions that ensure the required overall sulphur reduction.

Abstract: A process for hydroprocessing middle distillate petroleum streams in two temperature stages. The feedstream is hydroprocessed in two or more first temperature stages operated at a temperature from about 360.degree. C. to about 450.degree. C. The reaction product of the first temperature stage(s) is quenched to a temperature from about 260.degree. C. to about 350, stripped of H.sub.2 S, NH.sub.3 and other dissolved gases, then sent to the second temperature stage which is operated at said quenched temperature range. The product from the second temperature stage is also stripped of dissolved gases. Color bodies produced in the higher temperature first stage are hydrogenated in the last stage.

Abstract: An integrated process for treating pyrolysis gasolines by depentanizing the pyrolysis gasoline in a first distillation column reactor which also subjects the C.sub.5 fraction to selective hydrogenation of acetylenes and diolefins. The bottoms or C.sub.6 + material is then subjected to further distillation in a second distillation column reactor to remove either a C.sub.6 and lighter or C.sub.8 and lighter overheads which contains a benzene/toluene/xylene (BTX) concentrate while at the same time removing mercaptans and selectively hydrogenating the diolefins. The BTX concentrate is then subjected to hydrodesulfurization prior to aromatics extraction and separation of the benzene from the toluene and xylene. Concurrently with the benzene separation any remaining olef ins are saturated to remove the color bodies. Finally the heavy gasoline fraction is subjected to the concurrent catalytic removal of mercaptans and separation to remove the heaviest material.

Abstract: A method for producing a process oil is provided in which an aromatic extract oil is added to a paraffinic rich feed to provide a blended feed. The blended feed is then extracted with an aromatic extraction solvent to yield a raffinate which subsequently is hydrotreated to provide a process oil.

Abstract: A hydroprocessing process includes two cocurrent flow liquid reaction stages and one vapor stage, in which feed components are catalytically hydroprocessed by reacting with hydrogen. The liquid stages both produce a liquid and a hydrogen-rich vapor effluent, with most of the hydroprocessing accomplished in the first stage. The first stage vapor is also hydroprocessed. The hydroprocessed vapor and second stage vapor are cooled to condense and recover additional product liquid and produce an uncondensed hydrogen-rich vapor. After cleanup to remove contaminants, the hydrogen-rich vapor is recycled back into the first stage as treat gas. Fresh hydrogen is introduced into the second stage. This is useful for hydrotreating heteroatom-containing hydrocarbons.

Abstract: A process for transforming a gas oil cut into a dearomatized fuel with a high cetane number comprises at least one first, deep desulphurization and deep denitrogenation step in which the gas oil cut and hydrogen are passed over a catalyst comprising a mineral support, at least one group VIB metal or metal compound, at least one group VIII metal or metal compound, and phosphorous or at least one phosphorous compound, and at least one subsequent second step, dearomatization, in which the desulphurized and denitrogenated product from the first step is passed with hydrogen over a catalyst comprising a mineral support and at least one group VIII noble metal or noble metal compound.

Abstract: A three stage hydroprocessing process includes two liquid and one vapor reaction stages, with a hydrogen containing vapor effluent produced in both liquid stages. The second liquid stage vapor effluent comprises part of the first liquid stage feed and the first liquid stage vapor effluent is the feed for the vapor stage. At least a portion of the hydrogen for the first liquid stage and vapor stage reactions is respectively provided by the hydrogen in the second and first liquid stage vapor effluents.

Abstract: A method for producing a process oil is provided in which an aromatic extract oil is added to a paraffinic rich feed to provide a blended feed. The blended feed is then hydrotreated in a first hydrotreating stage to convert at least a portion of sulfur and nitrogen in the feed to hydrogen sulfide and ammonia. After stripping, the feed is subjected to a second hydrotreating stage to provide a process oil.

Abstract: A method and reactor for catalytic hydroprocessing liquid hydrocarbon feedstock at elevated temperatures and pressures for producing a liquid hydrocarbon product involves introducing the feedstock into a reactor having upper and lower reaction zones, each reaction zone having a hydroprocessing catalyst bed therein, the feedstock being introduced at the top of the lower reaction zone for downward flow through and reaction within the catalyst bed therein; collecting a partially reacted liquid effluent from the lower reaction zone; pumping the partially reacted liquid effluent to and introducing it at the top of the upper reaction zone for downward flow through and reaction within the catalyst bed therein; introducing hydrogen gas at the top of the upper reaction zone for flow downwardly and sequentially through and over the catalyst beds in the upper and lower reaction zones in co-current contact with the liquid in the reaction zones, the hydrogen reacting with the liquid in the reaction zones whereby the liqui

Abstract: Catalytic cracking gaseolines are treated by: (a) fractionating the raw gasoline cut into two cuts; (b) optional selective diene hydrodenation of the light cut, then mild hydrotreatment and stripping; (c) sweetening the light cut which is conducted before the mild hydrotreatment step by contact with a supported catalyst containing 0.1-1% by weight of palladium, or after the mild hydrotreatment step and which is then an extractive sweetening step, or with a catalyst having an alkaline base optionally incorporated and also an oxidizing agent. The heavy gaseoline fraction is optionally desilphurized in a hydrotreatment unit. The desulpurized and sweetened light gaesoline can be added to the gasoline pool either directly or mixed with the desulphurized heavy gaseoline cut.

Abstract: A process for converting a heavy hydrocarbon fraction comprises treating the hydrocarbon feed in a hydrodemetallization section, the section comprising at least one fixed bed hydrodemetallization catalyst.

Abstract: A hydroprocessing process for removing impurities from a feed comprising a hydrocarbonaceous liquid comprises at least two cocurrent, upflow hydroprocessing reaction stages and a non-catalytic, vapor-liquid contacting stage. The reaction and contacting stages may all be in the same reactor vessel. The feed and a hydrogen treat gas are passed up into a catalyst bed which comprises the first reaction stage, which produces a partially hydroprocessed liquid and vapor effluent. This first stage vapor is passed up into the contacting stage in which it contacts a hydrocarbonaceous liquid which reduces the vapor impurity content. The impurity-enriched contacting liquid passes down and mixes with the first stage liquid effluent. The combined effluents and hydrogen are passed up into the second reaction stage to form a processed product liquid and hydrogen-containing vapor effluent.

Abstract: A hydroprocessing process for removing impurities from a feed comprising a hydrocarbonaceous liquid comprises at least one cocurrent, upflow hydroprocessing reaction stage, a vapor-liquid contacting stage and a downflow hydroprocessing reaction stage. The feed and hydrogen react in the upflow stage to produce a partially hydroprocessed liquid and vapor effluent. The vapor contacts a hydrocarbonaceous liquid in the contacting stage, which transfers impurities from the vapor into the liquid. The impurity-enriched contacting liquid mixes with the upflow stage liquid effluent and the combined liquid effluents react with hydrogen in the downflow reaction stage, to form a hydroprocessed product liquid and vapor effluent. Additional product liquid is recovered by cooling and condensing either or both the contacting and downflow stage vapor effluents.

Abstract: A process for upgrading a liquid petroleum or chemical stream wherein said stream flows countercurrent to the flow of a treat gas, such as a hydrogen-containing gas, in at least one reaction zone. The reaction vessel used in the practice of the present invention contains vapor and optionally liquid passageway means to bypass one or more catalyst beds. This permits more stable and efficient reaction vessel operation.

Abstract: A process for hydrodesulfurizing naphtha feedstreams wherein the reactor inlet temperature is below the dew point of the feedstock at the reactor inlet so that the naphtha will completely vaporize within the catalyst bed. It is preferred to use a catalyst comprised of about 1 to about 10 wt. % MoO.sub.3, about 0.1 to about 5 wt. % CoO supported on a suitable support material. They are also characterized as having an average medium pore diameter from about 60 .ANG. to 200 .ANG.. a Co/Mo atomic ratio of about 0.1 to about 1.0, a MoO.sub.3 surface concentration of about 0.5.times.10.sup.-4 to about 3.0.times.10.sup.-4 g MoO.sub.3 /m.sup.2, and an average particle size of less than about 2.0 mm in diameter.

Abstract: The residue (bottoms) from a vacuum or atmospheric column is upgraded in a revamped multireactor hydrotreating zone. The hydrotreating zone is modified such that the entire effluent of the next to last reactor is withdrawn, light gases and hydrocarbons are removed from the effluent in separators and the remaining liquid is passed into a fractionation column and/or a carbon rejection zone. Gas oils and distillates from the column and/or carbon rejection zone are then returned to the last reactor of the hydrotreating zone.

Abstract: A hydrotreatment process for effecting hydrotreatment of a liquid hydrocarbon feedstock containing a mixture of liquid hydrocarbons together with organic sulphurous impurities in which a desulphurised liquid first hydrocarbon fraction is contacted with a first stream of desulphurised recycle gas to produce (A) a vaporous mixture including unreacted hydrogen, hydrogen sulphide, and a second hydrocarbon fraction including relatively more volatile components of the mixture of hydrocarbons and (B) a third liquid hydrocarbon fraction including relatively less volatile components of the mixture of hydrocarbons as well as residual sulphurous impurities, the vaporous mixture and the third liquid hydrocarbon fraction being recovered as separate streams from the contact zone. The third liquid hydrocarbon fraction is contacted with a mixture of make-up hydrogen-containing gas and desulphurised recycle gas to cause hydrodesulphurisation of residual sulphurous impurities in the third liquid hydrocarbon fraction.

Abstract: A hydroprocessing process includes two hydroprocessing reaction stages, both of which produce a liquid and a vapor effluent, and a liquid-vapor contacting stage. The first stage vapor effluent contains impurities, such as heteroatom compounds, which are removed from the vapor by contact with processed liquid effluent derived from one or both reaction stages and, optionally, also liquid recovered from processed vapor. The first and contact stage liquid effluents are passed into the second stage to finish the hydoprocessing. The contact and second stage vapor effluents are cooled to recover additional hydroprocessed product liquid.

Abstract: Disclosed herein is a highly efficient process for producing distillate fuels using a multi-bed hydrogenation reactor. The temperature of the feed to the second and subsequent reactor beds is controlled by removing effluent from the prior bed, cooling the effluent in an external heat exchanger, injecting hydrogen gas into the effluent mixture, and inserting the cooled mixture containing hydrogen gas into the inlet of the next reaction zone.

Abstract: The process for the conversion of heavy crude oils or distillation residues to distillates comprises the following steps:mixing the heavy crude oil or distillation residue with a suitable hydrogenation catalyst and sending the mixture obtained to a hydrotreating reactor introducing hydrogen or a mixture of hydrogen and H.sub.2 S;sending the stream containing the hydrotreating reaction product and the catalyst in slurry phase to a distillation zone where the most volatile fractions are separated;sending the high-boiling fraction obtained in the distillation step to a deasphaltation step obtaining two streams, one consisting of deasphalted oil (DAO), the other consisting of asphaltenes, catalyst in slurry phase, possibly coke and rich in metals coming from the initial charge;recycling at least 60%, preferably at least 80% of the stream consisting of asphaltenes, catalyst in slurry phase, optionally coke and rich in metals, to the hydrotreatment zone.

Abstract: A process for catalytic two-stage hydrodesulfurization of metal-containing petroleum residua feedstocks to achieve at least about 75% desulfurization of the liquid product while also providing at least about 40% reduction in catalyst consumption. In the process, used catalyst having a catalyst equilibrium age of 0.3-5.0 bbl oil feed/lb catalyst is withdrawn from the second stage reactor, rejuvenated so as to remove 10-50 wt. % of the contaminant metals and at least 80 wt. % of carbon deposited on the catalyst, and then cascaded forward and added to the first stage reactor. Sufficient fresh make-up catalyst is added to the second stage reactor to replace the used catalyst withdrawn there, and only sufficient fresh catalyst is added to the first stage reactor to replace any catalyst transfer losses. Used catalyst having a catalyst equilibrium age of 0.6 to 10.0 bbl. oil per lb. catalyst is withdrawn from the first stage reactor for discard.

Abstract: An aromatic solvent together with methods for its preparation are described. A composition includes a paraffin fraction in an amount of from approximately 9 LV % to approximately 15 LV %; a naphthene fraction in an amount of from approximately 35 LV % to approximately 55 LV %; and an alkylbenzene fraction in an amount of from approximately 8 LV % to approximately 16 LV %. The solvent provides advantages in that the high solvency that is typical of an aromatic solvent is combined with a narrow distillation range, a high flash point and higher boiling range that is typical of an aliphatic solvent.

Abstract: A process for desulfurizing catalytically cracked gasoline containing sulfur compounds and olefin components, which comprises the steps of:1) first desulfurizing the catalytically cracked gasoline in the presence of a hydrodesulfurization catalyst at a desulfurization rate of 60 to 90%, a reaction temperature of 200 to 350.degree. C., a hydrogen partial pressure of 5 to 30 kg/cm.sup.2, a hydrogen/oil ratio of 500 to 3,000 scf/bbl, and a liquid hourly space velocity of 2 to 10 1/hr, said first desulfuriing step comprising supplying a feed having a hydrogen sulfide vapor concentration of not more than 0.1% by volume, and2) next desulfurizing the treated oil obtained in the first step in the presence of a hydrodesulfurization catalyst at a desulfurization rate of 60 to 90%, a reaction temperature of 200 to 300.degree. C., a hydrogen partial pressure of 5 to 15 kg/cm.sup.

Abstract: A process for the simultaneous conversion of waste lubricating oil and pyrolysis oil derived from organic waste to produce a synthetic crude oil by means of contacting the combined feed with a hot hydrogen-rich gaseous stream to increase the temperature of the combined feed to vaporize at least a portion of the distillable organic compounds contained therein which is immediately hydrogenated in a hydrogenation reaction zone. The resulting effluent from the hydrogenation reaction zone is then introduced into a hydroprocessing zone to produce higher hydrogen-content hydrocarbons and to remove heterogeneous components such as sulfur, oxygen, nitrogen and halide, for example. The resulting effluent is cooled and partially condensed to produce a gaseous stream containing hydrogen and gaseous water-soluble inorganic compounds and a liquid stream containing hydrocarbon compounds.

Abstract: A process for producing a fuel oil base material having a lower sulfur content than that of stock oil and a dry sludge content of 0.05 mass % or less, which involves hydrotreating the stock oil having a dry sludge content of 0 to 5.0 mass % and a sulfur content of 1.0 to 10 mass % in two stages is provided, wherein the temperature of first-stage hydrotreatment is 340.degree. to 450.degree. C. and the temperature of second-stage hydrotreatment is 200.degree. to 440.degree. C. and maintained at a temperature lower than the temperature of the first-stage hydrotreatment.

Abstract: A hydrocarbon distillate fraction is hydrotreated in a single stage by passing the distillate fraction downwardly over a stacked bed of two hydrotreating catalysts. The catalyst in the upper bed contains 0.1 to 15% by weight of platinum and/or palladium and also contains 2 to 40% by weight of at least one of tungsten, chromium, a Group VIIB metal, and an actinium series metal supported on an acidic refractory oxide carrier. The catalyst in the lower bed contains 1 to 15% by weight of a non-noble Group VIII metal and 1 to 25% by weight of a Group VIB metal on an amorphous, refractory oxide carrier. The liquid hydrocarbon product recovered has a reduced content of aromatics and a reduced heteroatom content.

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: A method for producing a process oil is provided in which an aromatic extract oil is added to a napthenic rich feed. The combined feed is then hydrotreated in a first hydrotreating stage to convert at least a portion of sulfur and nitrogen in the feed to hydrogen sulfide and ammonia. After stripping the feed is subjected to a second hydrotreating stage to provide a process oil.

Abstract: A method for producing a process oil is provided in which an aromatic extract oil is added to a naphthenic rich feed to provide a blended feed. The blended feed is then extracted with an aromatic extract solvent to yield a raffinate which subsequently is hydrotreated to provide a process oil.

Abstract: A process for hydrotreating petroleum fractions early in the refining process by employing catalyst prepared as components of distillation structures or as contained beds of catalyst in atmospheric distillation columns and or side draw columns. For example, a crude petroleum is hydrotreated by taking side streams from an atmospheric distillation column and the vacuum gas oil from a vacuum distillation column which are individually fed to separate desulfurizations, preferably in distillation column reactors containing a hydrodesulfurization catalyst. The overheads from each of the distillation column reactors is returned to the atmospheric column and the bottoms from each distillation column reactor is withdrawn as hydrotreated product. The process may also be used for upgrading the effluent from a fluid catalytic cracking unit, preferably operated as a catalytic distillation reactor.

Abstract: A hydrotreating apparatus comprising (a') a fixed-bed reactor packed with a hydrotreating catalyst for hydrotreating a heavy oil and (b') a suspended-bed reactor packed with a hydrotreating catalyst for further hydrotreating the heavy oil hydrotreated in the fixed-bed reactor. According to the apparatus of the present invention, (a) feeding of a heavy oil to a fixed-bed reactor is disclosed packed with a hydrotreating catalyst to thereby effect hydrotreating of the heavy oil and (b) feeding of the heavy oil hydrotreated in the fixed-bed reactor to a suspended-bed reactor packed with a hydrotreating catalyst to thereby effect further hydrotreating of the heavy oil can be conducted, and therefore the period of hydrotreating of the heavy oil can be prolonged.

Abstract: There is provided a method of manufacturing gas oil containing low-sulfur and low-aromatic-compound content, said method including a first step of putting distilled petroleum to contact with hydrogen gas in the presence of a hydrotreating catalyst to reduce the sulfur concentration to not higher than 0.05 wt % and a second step of reducing the aromatic compound concentration in the presence of a noble metal type catalyst, with at least a pair of high temperature high pressure gas liquid separators arranged between the two steps to separate the gaseous and liquid components of distilled petroleum and hydrogen gas or hydrogen containing gas is introduced into the liquid component in each of the separators.

Abstract: A process for hydroprocessing liquid petroleum and chemical streams in two or more hydroprocessing stages, which stages are in separate reaction vessels and wherein each reaction stage contains a bed of hydroprocessing catalyst. The liquid product from the first reaction stage is sent to a stripping stage and stripped of H.sub.2 S, NH.sub.3 and other dissolved gases. The stripped product stream is then sent to the next downstream reaction stage, the product from which is also stripped of dissolved gases and sent to the next downstream reaction stage until the last reaction stage, the liquid product of which is stripped of dissolved gases and collected or passed on for further processing. The flow of treat gas is in a direction opposite the direction in which the reaction stages are staged for the flow of liquid. Each stripping stage is a separate stage, but all stages are contained in the same stripper vessel.

Abstract: A process for simultaneously removing heteroatoms, such as sulfur, from a virgin distillate stream and a light catalytic cyclic stream in two reaction zones in a hydrotreating process unit. One reaction zone will be a low temperature reaction zone and the other will be the high temperature zone. In the low temperature reaction zone, the cracked stream is reacted with a hydrotreating catalyst at a predetermined temperature and in high temperature reaction zone, the virgin distillate stream is reacted with a catalyst which is less reactive than that of the first reaction zone. When catalyst in the high reaction zone is replaced with fresh catalyst the temperature is lowered so that it now becomes the low temperature zone in which the cracked stream is redirected.

Abstract: A process for hydroprocessing liquid petroleum and chemical streams in a single reaction vessel containing two or more hydroprocessing reaction stages. The liquid product from the first reaction stage is stripped of H.sub.2 S, NH.sub.3 and other dissolved gases, then sent to the next downstream reaction stage. The product from the downstream reaction stage is also stripped of dissolved gases and sent to the next downstream reaction stage until the last reaction stage, the liquid product of which is stripped of dissolved gases and collected or passed on for further processing. The flow of treat gas is in a direction opposite the direction in which the reaction stages are staged for the flow of liquid.

Abstract: Disclosed is a process for hydroconverting a heavy hydrocarbon oil in a reactor under high-temperature and high-pressure conditions,wherein said hydroconversion is carried out through using at least three desulfurization catalysts which each contains as active metals transition metals of Group VI and VIII in the Periodic Table supported on an alumina carrier and which have different SI of 40 or higher, 30 or higher and below 40, and lower than 30, respectively,and wherein said at least three catalysts are packed into the reactor in a descending order of SI from the inlet to the outlet of the reactor, with the proportion of the catalyst having SI of 40 or higher is at least 10% by volume, that of the catalyst having SI of 30 or higher and below 40 is at least 20% by volume, and that of the catalyst having SI of lower than 30 is at least 30% by volume.

Abstract: A process is provided for converting a hydrocarbon feedstock comprising the steps of introducing the hydrocarbon feedstock to a first hydroconversion zone at superatmospheric pressure and at a temperature between about 450.degree. F. and about 850.degree. F. in the presence of hydrogen, the hydrogen flowing in a countercurrent relationship to the hydrocarbon feedstock, to form a hydrogen-rich vapor effluent and a hydrocarbon-rich liquid effluent; reacting the hydrogen-rich vapor effluent in a second hydroconversion zone to form a converted vapor effluent; and introducing a portion of the hydrocarbon-rich liquid effluent to the second hydroconversion zone in countercurrent relationship to the hydrogen-rich vapor effluent. By recycling to the second hydroconversion zone a stream having sufficiently high boiling range that it remains a liquid, a greater range of operating conditions are possible in the second hydroconversion zone, thus allowing for higher conversions and product yields.

Abstract: Heavy oils may be hydrotreated in the presence of a porous alumina support bearing metals of Group VIII, excluding cobalt, and VI-B and optionally phosphorus, the catalyst having a Total Surface Area of 240-320 m.sup.2 /g, a Total Pore Volume of 0.65-0.9 cc/g, and a Pore Diameter Distribution whereby 50-62.8% of the Total Pore Volume is present as micropores of diameter 55-115 .ANG. and 20-30.5% of the Total Pore Volume is present as macropores of diameter greater than 250 .ANG..The heavy oils and hydrogen are contacted with the catalyst such that the catalyst is maintained at isothermal conditions and is exposed to a uniform quality of feed. The process is particularly effective in achieving desired levels of hydroconversion of feedstock components having a boiling point greater than 1000.degree. F. to products having a boiling point less than 1000.degree. F.

Abstract: The present invention relates to a method of removing sulfur from a hydrotreating process stream comprising contacting a sulfur containing feedstock with a stacked bed catalyst system comprising a first catalyst bed comprising hydrodesulfurization catalysts followed by a second catalyst bed comprising ruthenium sulfide having a surface area of at least about 30 m.sup.2 /g and wherein said hydrodesulfurization process is conducted at a temperature of about 150.degree. C. to about 400.degree. C. and a pressure of about 50 psig (344.74 kPa) to about 2500 psig (17236.89 kPa).

Abstract: Spent or inactive alumina-supported catalysts removed from a catalytic hydrotreating process and having carbonaceous and metallic deposits thereon are reactivated. After a solvent wash to remove process oils, the spent catalyst is contacted with steam at a temperature of 1000.degree. to about 1250.degree. F. for a period of about 2 to about 5 hours to form a reactivated catalyst suitable for reuse in a catalytic hydrotreating process. Optionally, the steam-treated catalyst can be regenerated by contact with an oxygen-containing gas at a temperature of about 700.degree. to about 900.degree. F. to remove carbon deposits from the catalyst, or, alternatively, the steam-treated catalyst can be acid-leached to remove undesired metals and then contacted with an oxygen-containing gas at an elevated temperature to remove carbon deposits.

Abstract: The invention concerns a hydro treatment method in at least two stages, for a heavy hydrocarbon fraction containing asphaltenes, sulphur impurities and metallic impurities, wherein:a) in at least one first stage described as hydrodemetallization, the hydrocarbon charge and hydrogen are passed over a hydrodemetallization catalyst,b) in at least one subsequent stage described as hydrodesulphurization, the product of stage a) and hydrogen are passed over a hydrodesulphurization catalyst.The invention, in which the hydrodemetallization stage comprises one or more zones each containing hydrodemetallization catalyst operating in a fixed bed, is characterised in that this zone or these zones are preceded by two protective zones arranged in parallel, each containing a fixed bed of a hydrodemetallization catalyst, the two protective zones operating alternately.

Abstract: Low sulfur distillate fuel oils such as road diesel oil having a maximum sulfur content of 0.05 weight percent, are produced by segregation of a distillate range feed into a lower boiling fraction and higher boiling fraction with the cut point between the two fractions between about 600.degree. and 650.degree. F. (about 315.degree. to 345.degree. C.). The higher boiling fraction is hydrodesulfurized under relatively severe conditions and then combined with the lower boiling fraction to be hydrodesulfurized under less severe conditions. Operation in this manner enables the refractory dibenzothiophenes to be removed while maintaining a lower hydrogen consumption.

Abstract: Diesel fuels are decolorized by hydrotreatment under mild conditions. The feedstock is normally severely hydrotreated to convert organosulfur or organonitrogen and the effluent passed to a smaller downstream hydrotreating zone at a lower temperature but sufficient to lighten the color of a finished product hydrocarbon.

Abstract: Heavy oils are advantageously preconditioned by heat soaking prior to hydrotreating with a dispersed metal catalyst to reduce coking in a two stage hydrotreating process. The effluent of a hydrotreating process is filtered to recover catalytically active coke which is recovered by backflushing and recycled to the feed stream. A mild solvent deasphalting step isolates metals in a reduced volume asphaltene fraction.

Abstract: There is provided a process for upgrading hydrocarbon feedstocks, such as resids or shale oil. The process uses a catalyst comprising at least one Group VIA or Group VIII metal, such as nickel and molybdenum, and an ultra-large pore oxide material. The ultra-large pore oxide material is used in decreasing pore size from top to bottom of the reactor.

Abstract: A process for the production of a low-sulfur diesel gas oil having a sulfur content of 0.05% by weight or lower and having a Saybolt color number of -10 or higher, from a petroleum distillate having a sulfur content of 0.1 to 2.0% by weight and having an inferior color and inferior oxidation stability comprises contacting the petroleum distillate with hydrogen in the presence of a hydro-treating catalyst which has at least one metal supported on said porous carrier, at a temperature of 350.degree. to 450.degree. C., and a pressure of 45 to 100 kg/cm.sup.2 in the first step to thereby produce materials having a sulfur content of 0.05% by weight or lower, and contacting further the materials issued from the first step with hydrogen in the presence of a hydro-treating catalyst which has at least one metal supported on said porous carrier, at a temperature of 200.degree. to 300.degree. C., and a pressure of 45 to 100 kg/cm.sup.2 in the second step to thereby produce the finished low-sulfur diesel gas oil.

Abstract: The production of food grade quality white mineral oils from predominantly naphthenic or cycloparaffinic crude distillates heretofore have required acid treating using sulfuric acid followed by neutralization, water wash and possibly finishing step. Herein, however, three stages of hydroprocessing without any solvent extraction or acid treatment prior step are employed to produce the desired food grade quality white mineral oil having a trace of aromatic constituents therewithin. Specific steps are defined in the application in terms of the severity of the hydrogenation in the hydrotreatiang operation at each respective step; as well as the steps of separating gaseous constituents of the hydroprocessing product.

Abstract: Liquid sulphur-containing hydrocarbon feedstock is passed through two or more hydrodesulfurization zones and connected in a series each containing a packed bed of solid sulfurized catalyst. The liquid is passed from the first zone to the next until the final zone. Make up hydrogen is supplied to a hydrodesulfurization zone (i) other than the first hydrodesulfurization zone; hydrogen-containing gas is recovered from each hydrodesulfurization zone. The first hydrodesulfurization zone is supplied with hydrogen-containing gas recovered from a subsequent hydrodesulfurization zone. Hydrogen-containing gas recovered from the first hydrodesulfurization zone is purged. Liquid material recovered from the first hydrodesulfurization zone is recycled to the inlet of the hydrosulfurization zone so as to provide diluent for admixture with liquid feedstock.