Abstract: A dual riser FCC process for converting C3/C4-containing feedstocks to aromatics. First and second hydrocarbon feeds (5, 6) are supplied to the respective first and second risers (2, 4) in a dual-riser FCC unit with a gallium enriched catalyst to make an effluent rich in ethylene, propylene and aromatics. The first riser (2) is operated at less severe conditions than the second riser (4) and can receive a relatively heavy feed such as gas oil. The feed to the second riser (4) includes propane, for example LPG, propane recycle from the C3 splitter (72), etc. The FCC catalyst can include gallium to promote aromatics formation.

Abstract: The present invention concerns an apparatus and associated process for the catalytic cracking of oil cuts in a fluidized bed. The apparatus and process can catalytically crack a conventional feed in a principal riser B and crack a secondary feed in at least one secondary riser C. The lower end of the secondary riser or risers C is open to the bottom portion of the principal riser B; the upper end of the secondary riser or risers C is open to the top portion of the principal riser B.

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 process for the hydroprocessing of multiple feedstreams including vacuum gas oil and light cycle oil. The light cycle oil is reacted with hydrogen in a hydrocracking zone and the hydrocarbon feedstream comprising vacuum gas oil is reacted with hydrogen in a hydrodesulfurization reaction zone. The hydrotreated vacuum gas oil is good FCC feedstock. Naphtha and ultra low sulfur diesel are recovered in a common fractionation column.

Abstract: The present invention relates to a thermo catalytic process to produce diesel oil from vegetable oils, in refineries which have two or more Catalytic Cracking (FCC) reactors. At least one reactor processes heavy petroleum or residue in conventional operation conditions while at least one reactor processes vegetable oils in proper operation conditions to produce diesel oil. This process employs the same catalyst employed in the FCC process, which processes conventional feedstocks simultaneously. This process transforms high heat content raw materials into fuel hydrocarbons. It may improve efficiency for the obtainment of highly pure products and may not yield glycerin, one by-product of the transesterification process. The diesel oil produced by said process may have superior qualities and/or a cetane number higher than 40. Once cracking conditions occur at lower temperatures, it may form a less oxidized product, which is consequently purer than those obtained by existent technology.

Abstract: A shell-and tube reactor including at least one reaction tube with a measuring means, substantially same solid particles being filled in the reaction tubes with or without the measuring means, a length of the filled solid particle layer, and a pressure drop thereof while passing a gas through the reaction tube, per each reaction tube, being substantially the same, respectively. By measuring the temperature of the catalyst particle layer, such a temperature as a representative can be gasped.

Abstract: Process for the production of hydrocarbon blends with a high octane number by the hydrogenation of hydrocarbon blends, containing branched C8, C12 and C16 olefinic cuts, characterized by sending said blends, as such or fractionated into two streams, one substantially containing the branched C8 olefinic cut, the other substantially containing the branched C12 and C16 olefinic cuts, to a single hydrogenation zone or to two hydrogenation zones in parallel, respectively, only the stream substantially containing of saturated C8 hydrocarbons, obtained by the fractionation of the stream produced by the single hydrogenation zone or obtained by the hydrogenation zone fed by the fractionated stream substantially containing the branched C8 olefinic cut, being at least partly recycled to the single hydrogenation zone or to the hydrogenation zone fed by the fractionated stream substantially containing the branched C8 olefinic cut, and the hydrocarbon blend with a high octane number, obtained by the fractionation of the st

Abstract: The present invention relates to a process for the conversion of hydrocarbon streams with 95% true boiling point less than 400° C. to very high yield of liquefied petroleum gas in the range of 45-65 wt % of feed and high octane gasoline, the said process comprises catalytic cracking of the hydrocarbons using a solid fluidizable catalyst comprising a medium pore crystalline alumino-silicates with or without Y-zeolite, non crystalline acidic materials or combinations thereof in a fluidized dense bed reactor operating at a temperature range of 400 to 550° C., pressure range of 2 to 20 kg/cm2 (g) and weight hourly space velocity in range of 0.1 to 20 hour?1, wherein the said dense bed reactor is in flow communication to a catalyst stripper and a regenerator for continuous regeneration of the coked catalyst in presence of air and or oxygen containing gases, the catalyst being continuously circulated between the reactor-regenerator system.

Abstract: Process for the work-up of naphtha, wherein a) naphtha or a stream produced from naphtha in a pretreatment step is separated in a membrane unit into a stream A which is depleted in aromatics and a stream B which is enriched in aromatics, with the aromatics concentration in stream A being from 2 to 12% by weight (step a), b) at least part of the substream A is fed to a steam cracker (step b), c) at least part of the substream B is fed to a unit in which it is separated by means of a thermal process into a stream C which has a lower aromatics content than stream B or a plurality of streams C?, C?, C?? . . . which each have lower aromatics contents than stream B and a stream D which has a higher aromatics content than stream B or a plurality of streams D?, D?, D?? . . .

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 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: A dual riser FCC process for converting C3/C4-containing feedstocks to aromatics. First and second hydrocarbon feeds (5, 6) are supplied to the respective first and second risers (2, 4) in a dual-riser FCC unit with a gallium enriched catalyst to make an effluent rich in ethylene, propylene and aromatics. The first riser (2) is operated at less severe conditions than the second riser (4) and can receive a relatively heavy feed such as gas oil. The feed to the second riser (4) includes propane, for example LPG, propane recycle from the C3 splitter (72), etc. The FCC catalyst can include gallium to promote aromatics formation.

Abstract: A process for the production of low sulfur diesel and high octane naphtha.

Abstract: The present invention is generally related towards enhancing the yield and/or cold-flow properties of certain hydrocarbon products, increasing the degree of isomerization in a diesel product and/or increasing the production rate of a diesel product. The embodiments generally include reducing the residence time of lighter hydrocarbon fractions during hydrocracking, thereby decreasing secondary cracking, by various configurations of introducing at least two hydrocarbon feedstreams of different boiling ranges at different entry points in a hydrocracking unit. A method further includes forming a hydrocarbons stream comprising primarily C5+ Fischer-Tropsch hydrocarbon products; fractionating hydrocarbons stream to form at least a wax fraction and an intermediate fraction which serve as separate feedstreams to a hydrocracking unit comprising at least two hydroconversion zones.

Abstract: A reactor apparatus and process for contacting hydrocarbons with catalyst. The reactor apparatus comprises a plurality of tubular reactors each having a first end into which a catalyst is fed and a second end through which the catalyst and product exit the tubular reactor. A catalyst retention zone is provided to contain catalyst and feed catalyst to the tubular reactors. A separation zone is provided to separate the catalyst from products of a reaction conducted in the apparatus. A transport conduit having a first end in fluid communication with the second ends of at least two of the tubular reactors and a second end extending into the separation zone transports product and catalyst to the separation zone. A catalyst return in fluid communication with the separation zone and the catalyst retention zone returns catalyst to the catalyst retention zone.

Abstract: The invention concerns a process for producing middle distillates from effluents obtained from the Fischer-Tropsch process, comprising separating a heavy cut with an initial boiling point of 120-200° C., hydrotreating said cut and fractionating the hydrotreated cut to obtain at least one intermediate fraction and at least one fraction that is heavier than the intermediate fraction. The intermediate fraction boils between T1 and T2, T1 being in the range 120-200° C. and T2 being in the range 300-410° C. The heavy and intermediate fractions are treated over a hydrocracking/hydroisomerisation catalyst and the effluents obtained are distilled. The invention also concerns a unit.

Abstract: A distillate fuel steam reformer system in which a fuel feed stream is first separated into two process streams: an aliphatics-rich, sulfur-depleted gas stream, and an aromatics- and sulfur-rich liquid residue stream. The aliphatics-rich gas stream is desulfurized, mixed with steam, and converted in a reforming reactor to a hydrogen-rich product stream. The aromatics-rich residue stream is mixed with air and combusted to provide heat necessary for endothermic process operations. Reducing the amounts of sulfur and aromatic hydrocarbons directed to desulfurzation and reforming operations minimizes the size and weight of the overall apparatus. The process of the invention is well suited to the use of microchannel apparatuses for heat exchangers, reactors, and other system components, which may be assembled in slab configuration, further reducing system size and weight.

Abstract: The present invention relates to a catalytic cracking process and a device used in the process in particular, the present invention provides a catalytic cracking process, which comprises which comprises: 1) catalytic cracking a feedstock in the first riser for less than about 1.5 second and sending the resultant stream into the first separating device,; 2) catalytic cracking the recycle oil obtained from the first separating device in the second riser for less than about 1.

Abstract: This invention relates to a novel integrated method for economically processing vacuum residue from heavy crude oils. This is accomplished by utilizing a solvent deasphalter (SDA) in the first step of the process with a C3/C4/C5 solvent such that the DAO product can thereafter be processed in a classic fixed-bed hydrotreater or hydrocracker. The SDA feed also includes recycled stripper bottoms containing unconverted residue/asphaltenes from a downstream steam stripper unit. The asphaltenes from the SDA are sent to an ebullated-bed reactor for conversion of the residue and asphaltenes. Residue conversion in the range of 60-80% is achieved and asphaltene conversion is in the range of 50-70%. The overall residue conversion, with the DAO product considered non-residue, is in the range of 80 W %-90 W % and significantly higher than could be achieved without utilizing the present invention.

Abstract: The present invention relates to a process for selectively producing C3 olefins from a catalytically cracked or thermally cracked naphtha stream by fractionating the naphtha feed to obtain at least a C6 rich fraction and feeding the C6 rich fraction into a reaction stage at a point wherein the residence time of the C6 rich fraction is minimized.

Abstract: The present invention relates to a process for selectively producing C3 olefins from a catalytically cracked or thermally cracked naphtha stream by fractionating the naphtha feed to obtain a C6 fraction and feeding the C6 fraction either in the riser downstream of the injection point for the reminder of the naphtha feed, in the stripper, and/or in the dilute phase immediately downstream or above the stripper of a process unit.

Abstract: The propylene production of a fluid catalytic cracking unit employing a large pore zeolite cracking catalyst, produces more propylene by adding a naphtha cracking riser and a medium pore zeolite catalytic component to the unit, and recycling at least a portion of the naphtha crackate to the naphtha riser. The large pore size zeolite preferably comprises a USY zeolite and the medium pore size is preferably ZSM-5. Propylene production per unit of naphtha feed to the naphtha riser is maximized, by using the 60–300° F. naphtha crackate as the feed.

Abstract: An apparatus and a process for catalytic cracking of a hydrocarbon feed is described, carried out in at least two reaction zones, one (30) operating in catalyst riser mode, wherein the feed and catalyst from regeneration zone (3) are circulated from bottom to top, the first gases produced are separated from the coked catalyst in a first separation zone (38), the catalyst is stripped (40), a first cracking and stripping effluent (42) is recovered and the coked catalyst is recycled (45) to the regeneration zone. Catalyst (12) from regeneration zone (3) and a hydrocarbon feed (19) are introduced into the upper portion of a dropper reaction zone (16), the catalyst and feed being circulated from top to bottom, the coked catalyst is separated from the second gases produced in a second separation zone (20), the second gases (24) produced are recovered and the coked catalyst is recycled (25) to the regeneration zone.

Abstract: This invention relates to a novel method for economically processing vacuum residue from heavy crude oils by selectively processing the difficult and easy components in reactors whose design and operating conditions are optimized for the specific feed. The process utilizes an integrated solvent deasphalting (SDA)/ebullated-bed design wherein the heavy vacuum residue feedstock is initially sent to an SDA unit operated with C4/C5 solvent to achieve a high deasphalted oil (DAO) yield. The resulting SDA products, namely asphaltenes and DAO are separately treated in ebullated-bed reactor(s) systems whose design and operating conditions are optimized for a particular feedstock. The resulting net conversion, associated distillate yield and product qualities are greatly improved relative to treatment of the entire residue feedstock in a common ebullated-bed reactor system.

Abstract: A method for producing lubricant base oils is provided comprising the steps of: (a) separating a feedstock into a light lubricant base oil fraction and a heavy fraction; (b) hydroisomerizing the fractions over a medium pore size molecular sieve catalyst under hydroisomerization conditions to produce an isomerized light lubricant base oil fraction having a pour point less than or equal to a target pour point of the lubricant base oils and an isomerized heavy fraction having a pour point of equal to or greater than the target pour point of the lubricant base oils and a cloud point greater than the target cloud point of the lubricant base oils; and (c) dehazing the isomerized heavy fraction to provide a heavy lubricant base oil having a pour point less than or equal to the target pour point of the lubricant base oils and a cloud point less than or equal to the target cloud point of the lubricant base oils.

Abstract: Hydroprocessing such as hydrocracking is advantageously employed in processes for the recovery and purification of higher diamondoids from petroleum feedstocks. Hydrocracking and other hydroprocesses degrade nondiamondoid contaminants.

Abstract: A system comprising: a paraffin feed produced by the Fischer-Tropsch process is fractionable into at least three fractions: an intermediate fraction boiling between T1 and T2, T1 being in the range 120–200° C. and T2 being more than 300° C. and less than 410° C., a light fraction boiling below it and a heavy fraction boiling above it; at least a portion of the intermediate fraction is hydrotreated then at least a portion thereof is passed over an amorphous hydroisomerisation/hydrocracking catalyst; the heavy fraction is passed over an amorphous hydroisomerisation/hydrocracking catalyst with a conversion of 370° C.+ products into 370° C.? products of more than 80% by weight; the hydrocracked/hydroisomerised fractions are distilled to obtain middle distillates (kerosine, gas oil).

Abstract: Integration of gas oil and light olefin catalytic cracking zones with a pyrolytic cracking zone to maximize efficient production of petrochemicals is disclosed. Integration of the units in parallel allows production of an overall product stream with maximum ethylene and/or propylene by routing various feedstreams and recycle streams to the appropriate cracking zone(s), e.g. ethane/propane to the steam pyrolysis zone and C4 C6 olefins to the light olefin cracking zone. This integration enhances the value of the material balances produced by the integrated units.

Abstract: A process for the production of low sulfur hydrocarbonaceous products. The hydrocarbon feedstocks are processed in integrated desulfurization zone, hydrocracking and hydrogenation zones to produce ultra low sulfur diesel, low sulfur naphtha products and low sulfur heavy distillate.

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: The present invention is directed to a hydrocarbon conversion apparatus and process. The apparatus comprises the following: a plurality of riser reactors, each having a first end into which a catalyst is fed, a second end through which the catalyst can exit, and optionally a center axis extending therebetween. The apparatus also includes a separation zone having a plurality of inlets, each inlet not being oriented along the center axes of the riser reactors, the separation zone being provided to separate the catalyst from products of a reaction conducted in the hydrocarbon conversion apparatus. A plurality of deviating members are also provided, each deviating member being in fluid communication between the second end of a respective riser reactor and a respective inlet of the separation zone. The apparatus also includes a catalyst retention zone provided to contain catalyst, which is fed to the riser reactors.

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: A defined catalyst withdrawal and replacement program for optimizing the productivity and the economics of catalyst consumption in a multi-reactor system is disclosed. Catalyst cost is reduced by minimizing removal of the newest catalyst and maximizing removal of older catalyst to achieve an overall reduction of catalyst age in the multi-reactor system.

Abstract: A reactor apparatus and process for contacting hydrocarbons with catalyst. The reactor apparatus comprises a plurality of tubular reactors each having a first end into which a catalyst is fed and a second end through which the catalyst and product exit the tubular reactor. A catalyst retention zone is provided to contain catalyst and feed catalyst to the tubular reactors. A separation zone is provided to separate the catalyst from products of a reaction conducted in the apparatus. A transport conduit having a first end in fluid communication with the second ends of at least two of the tubular reactors and a second end extending into the separation zone transports product and catalyst to the separation zone. A catalyst return in fluid communication with the separation zone and the catalyst retention zone returns catalyst to the catalyst retention zone.

Abstract: According to this invention, there is provided a process and apparatus for catalytic cracking of various petroleum based heavy feed stocks in the presence of solid zeolite catalyst and high pore size acidic components for selective bottom cracking and mixtures thereof, in multiple riser type continuously circulating fluidized bed reactors operated at different severities to produce high yield of middle distillates, in the range of 50–65 wt % of fresh feed.

Abstract: A process and apparatus is disclosed for contacting feed with mixed catalyst in a secondary reactor that is incorporated into an FCC reactor. The mixed catalyst used in the secondary reactor is regenerated catalyst from a regenerator that regenerates spent catalyst from an FCC reactor that is mixed with spent catalyst from either the FCC reactor or the secondary reactor. The mixing of spent and regenerated catalyst reduces the catalyst temperature and tempers catalyst activity to inhibit both thermal and catalytic cracking reactions.

Abstract: A wide cut Fischer-Tropsch derived diesel fuel is produced wherein the distillate boils in a wider range than a conventional diesel fuel while providing favorable low temperature properties and environmentally beneficial effects. In particular, the fuel comprises a hydrocarbon distillate derived from the Fischer-Tropsch process having T90 greater than 640° F. (338° C.) but less than 1000° F. (538° C.) and a cold filter plugging point less than or equal to +5° C.

Abstract: A process is described for fluid catalytic cracking of hydrocarbons with high levels of basic nitrogen, where hydrocarbon feedstocks A and B with different levels of basic nitrogen are injected in a segregated fashion, into different risers of a multiple riser FCCU that possesses at least two risers. The injection of the feedstocks is made in such a way that feedstock A, to be injected in the riser with greater volume—main riser 7—possessing a level of basic nitrogen at least 200 ppm lower than the level of feedstock B to be injected into the riser with lower volume—secondary riser (8).

Abstract: A process for cracking, in a fluidized bed, a hydrocarbon charge wherein the cooling particles, which may optionally also be catalytic particles, circulate in two successive reaction chambers (1; 16), in each of which they are brought into contact with at least one cut of hydrocarbons, and the reaction effluents from each of the chambers are directed towards one and the same fractionating unit. The effluents from each of the reaction chambers (1; 16) are fractionated in part separately in one and the same partially partitioned fractionating unit, and at least one cut (12) obtained by separately fractionating the effluents from one of the two reaction chambers (1; 16) is, as a whole or in part, reinjected into the other chamber.

Abstract: Heavy hydrocarbons are upgraded to higher value distillates in a hydrocarbon conversion process which employs several parallel on-stream reaction zones which each contain both hydrotreating and hydrocracking catalyst beds. The feed and liquid recycled from the bottom of the reaction zone is charged to the top of the uppermost catalyst bed. Hydrogen flow in the reaction zones is countercurrent to the descending liquid, and products are removed as vapor. The flow of feed to one of the reaction zones is periodically stopped to allow sequential on-stream hydrogenative regeneration of the catalysts within the reaction zones. This allows continuous commercial operation at conditions which are otherwise unfeasible.

Abstract: This invention relates to a multi-stage process for hydroprocessing gas oils. Preferably, each stage possesses at least one hydrocracking zone. The second stage and any subsequent stages possess an environment having a low heteroatom content. Light products, such as naphtha, kerosene and diesel, may be recycled from fractionation (along with light products from other sources) to the second stage (or a subsequent stage) in order to produce a larger yield of lighter products, such as gas and naphtha. Subsequent zones are maintained at a lower pressure than that of the first zone, thereby reducing operating expenses.

Abstract: A method for processing a gasoline range hydrocarbon stream wherein a single reactor/distillation tower stream is fractionated into a light fraction and a heavy fraction, the light fraction is hydrodesulfurized, the heavy fraction is optionally hydrocracked and then hydrodesulfurized, and the light and heavy fractions are separately recovered.

Abstract: An entrained bed or fluidised bed process for catalytic cracking of a hydrocarbon feed in two reaction zones is described, one zone (1) being in catalyst dropper mode, the other (2) being in catalyst riser mode. A feed (102) and catalyst from at least one regeneration zone (302) are introduced into the upper portion of the dropper zone, the feed and catalyst are circulated in accordance with a catalyst to feed weight ratio, C/O, of 5 to 20, the cracked gases are separated from the coked catalyst in a first separation zone (105), the cracked gases are recovered (107), the coked catalyst is introduced (110) into the lower portion of the riser zone (2), the coked catalyst and said feed are circulated in a C/O weight ratio of 4 to 8, the used catalyst is separated from the effluent produced in a second separation zone (203), the catalyst is stripped in a stripping zone (212), the effluent and stripping gases are recovered (206) and the used catalyst is recycled (7) to the regeneration zone.

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: A process for increasing the yield of C10 plus hydrocarbon products from a Fischer-Tropsch plant which comprises the steps of (a) separating a Fischer-Tropsch product into a wax fraction and a condensate fraction; (b) dewaxing the wax fraction to produce a high boiling intermediate; (c) hydrofinishing the high boiling intermediate; (d) dehydrating the alcohols in the condensate fraction to convert them into olefins; (e) oligomerizing the olefins to form higher molecular weight hydrocarbons; (f) hydrofinishing the oligomerization mixture; and (g) and recovering a C10 plus hydrocarbon product from the hydrofinishing zone.

Abstract: A process for increasing the yield of C10 plus hydrocarbon products from a Fischer-Tropsch plant which comprises the steps of (a) separating a Fischer-Tropsch product into a wax fraction and a condensate fraction; (b) dewaxing the wax fraction to produce a high boiling intermediate; (c) hydrofinishing the high boiling intermediate; (d) dehydrating the alcohols in the condensate fraction to convert them into olefins; (e) oligomerizing the olefins to form higher molecular weight hydrocarbons; (f) hydrofinishing the oligomerization mixture; and (g) and recovering a C10 plus hydrocarbon product from the hydrofinishing zone.

Abstract: A process for upgrading at least one of a Fischer-Tropsch naphtha and a Fischer-Tropsch distillate to produce at least one of a gasoline component, a distillate fuel or a lube base feedstock component. The process includes reforming a Fischer-Tropsch naphtha to produce hydrogen by-product and a gasoline component with a research octane rating of at least about 80. The process further includes upgrading a Fischer-Tropsch distillate using the hydrogen by-product to produce a distillate fuel and/or a lube base feedstock component.

Abstract: A novel apparatus for producing sweet synthetic crude from a heavy hydrocarbon feed comprising: an upgrader for receiving said heavy hydrocarbon feed and producing a distillate fraction including sour products, and high-carbon content by-products; a gasifier for receiving the high-carbon content by-products and producing synthetic fuel gas and sour by-products; a hydroprocessing unit for receiving the sour by-products and hydrogen gas, thereby producing gas and sweet crude; and a hydrogen recovery unit for receiving said synthetic fuel gas and producing further hydrogen gas and hydrogen-depleted synthetic fuel gas, said further hydrogen gas being supplied to said hydroprocessing unit.

Abstract: The two-stage hydrocracking process of the present invention comprises bringing the first-stage feed oil containing a hydrocarbon component and having a boiling point of 316° C. or higher into contact with the first-stage catalyst in the presence of hydrogen to obtain a first-stage product; separating the first-stage product into heavy component and light component containing the middle distillate products; bringing the second-stage feed oil containing heavy component of the first-stage reaction product into contact with the second-stage catalyst in the presence of hydrogen to obtain the second-stage product; separating the second-stage product into heavy component and light component comprising middle distillate products and recycling part of the heavy component of the second-stage product to the second-stage feed oil. Hydrocracking activity of the first-stage catalyst is higher than hydrocracking activity of the second-stage catalyst.