Abstract: A process and apparatus are disclosed for hydrotreating a hydrocarbon feed in a hydrotreating unit and hydrocracking a second hydrocarbon stream in a hydrocracking unit. The hydrocracking unit and the hydrotreating unit may share the same recycle gas compressor. A make-up hydrogen stream may also be compressed in the recycle gas compressor. The second hydrocarbon stream may be a diesel stream from the hydrotreating unit. The diesel stream may be a diesel and heavier stream from a bottom of a hydrotreating fractionation column.

Abstract: Methods are provided for producing a jet fuel composition from a feedstock comprising a natural oil. The methods comprise reacting the feedstock with oxygen under conditions sufficient to form an oxygen-cleaved product. The methods further comprise hydrogenating the oxygen-cleaved product under conditions sufficient to form a jet fuel composition.

Abstract: This disclosure relates to liquid-full processes for hydroprocessing a light cycle oil (LCO). The processes involve hydrotreatment followed by selective ring opening in the presence of hydrotreating catalyst and selective ring opening catalyst respectively. The selective ring opening catalyst can be either zeolite ring opening catalyst or amorphous ring opening catalyst. In aspects of zeolite ring opening catalyst, the volume ratio of the total amount of the zeolite ring opening catalyst to the total amount of the hydrotreating catalyst is from about 0.2 to about 1.5. In aspects of amorphous ring opening catalyst, the volume ratio of the total amount of the amorphous ring opening catalyst to the total amount of the hydrotreating catalyst is from about 0.2 to about 3.

Abstract: A process and apparatus are disclosed for hydrotreating a hydrocarbon feed in a hydrotreating unit and hydrocracking a second hydrocarbon stream in a hydrocracking unit. The hydrocracking unit and the hydrotreating unit may share the same recycle gas compressor. A make-up hydrogen stream may also be compressed in the recycle gas compressor. A hydrocracking separator separates recycle gas and hydrocarbons from the hydrocracking unit to be processed with effluent from the hydrotreating unit.

Abstract: Integrated hydroprocessing methods using high activity, low density catalysts are provided. The high activity catalysts allow for blocked operation when processing lube range feedstocks of widely varying characteristics, such as wax content, without having to substantially change the configuration or operating conditions of the process train. Instead, the different feedstocks can be accommodated by varying the reaction temperature in the process train.

Abstract: Integrated hydroprocessing methods using high activity, low density catalysts are provided. The high activity catalysts allow for lower temperature operation, which reduces catalyst degradation, while the low density of the catalysts means a corresponding reduction in the amount of metal needed to fill a reactor volume. The methods allow for flexible processing of feedstocks with a variety of wax contents.

Abstract: A divided wall column allows for fractionation of multiple streams while maintaining separate product qualities. Effluents from multiple stages of a reaction system can be processed in a single divided wall column. The divided wall column can produce multiple cuts from each separated area, as well as at least one output from a common area.

Abstract: The present invention relates to a method for preparing lubricating base oils by using vacuum distilled deasphalted oil, and more specifically, to a method for preparing various kinds of lubricating base oils by distilling a distillate obtained from a solvent deasphalting (SDA) process under reduced pressure to obtain heavy deasphalted oil (H-DAO) and light deasphalted (Lt-DAO) and then treating the H-DAO and the Lt-DAO by catalytic reactions, respectively. According to the present invention, it is possible to obtain heavy lubricating base oil (150BS) of a high viscosity grade which can not be obtained by a known catalytic reaction and a lubricating base oil of group III by hydrogenation, in a high yield, and thus economical efficiency is excellent.

Abstract: This invention provides methods for multi-stage hydroprocessing treatment of FCC naphthas for improving the overall production quantity of naphtha boiling-range materials during naphtha production for low sulfur gasolines. Of particular benefit of the present processes is the selective treating of cat naphthas to remove gums instead of undercutting the overall naphtha pool by lowering the end cutpoints of the cat naphtha fraction. This maximizes the amount of refinery cat naphtha that can be directed to the gasoline blending pool while eliminating existing processing problems in hydrodesulfurization units. The processes disclosed herein have the additional benefit of minimizing octane losses in the increased naphtha pool volume.

Abstract: The method for manufacturing a hydrocarbon oil of the present invention comprises a first step wherein a plurality of reaction zones filled with a specific catalyst is disposed in series and a feedstock oil containing an oxygen-containing hydrocarbon compound derived from an animal or vegetable oil is supplied and hydrotreated under the conditions of a hydrogen pressure of 1 MPa or more and 10 MPa or less in each of the reaction zones; and a second step wherein hydrogen, hydrogen sulfide, carbon dioxide and water are removed from a product to be treated obtained in the first step to obtain a hydrocarbon oil. Among the plurality of reaction zones, the inlet temperature of the reaction zone disposed on the most upstream side is 150° C. or more and 250° C. or less, the inlet temperature of the second most upstream reaction zone or below is equal to or higher than the condensation temperature of water, and the outlet temperature of the reaction zone disposed on the most downstream side is 260° C.

Abstract: For conversion of crude oil or a heavy hydrocarbon fraction having an initial boiling point of at least 300° C., conducting a catalytic hydroconversion in a three-phase reactor operating in a boiling bed with an upward flow of liquid and gas, separating resultant effluent into a light liquid fraction boiling at less than 300° C. and a heavy liquid fraction boiling above 300° C., deasphalting the heavy liquid fraction to obtain a deasphalted hydrocarbon fraction and residual asphalt, and recycling at least one portion of the deasphalted hydrocarbon fraction upstream of the hydroconversion stage.

Abstract: Conversion of a heavy hydrocarbon fraction that is obtained either from a crude oil or from the distillation of a crude oil and that has an initial boiling point of at least 300° C. by hydroconversion of at least one portion of heavy hydrocarbon fraction in the presence of hydrogen in at least one three-phase reactor containing at least one hydroconversion catalyst, separation of the effluent to obtain a light liquid fraction that boils at a temperature that is less than 300° C. and a heavy liquid fraction that boils at a temperature that is greater than 300° C., and a deasphalting of at least one portion of the heavy liquid fraction that boils at a temperature that is greater than 300° C.

Abstract: The present invention relates to a process for desulfurizing heavy oil feedstreams with alkali metal compounds and improving the compatibility of the to stream components in either the feed stream, an intermediate product stream, and/or the reaction product stream in the desulfurization process. The present invention utilizes a high stability aromatic-containing stream that is preferably added to the heavy oil prior to reaction with the alkali metal compounds. The resulting stream resists precipitation of reaction solids in the desulfurization reactors. Even more preferably, the desulfurization system employs at least two desulfurization reactors in series flow wherein the high stability aromatic-containing stream is contacted with the reaction product from the first reactor prior to the second reactor, wherein the first reactor can be operated at a higher severity than without the use of the high stability aromatic-containing component stream.

Abstract: The present invention relates to quenching, during hydroprocessing of a hydrocarbon feed stream. More particularly, the present invention provides for quenching in hydroprocessing of a hydrocarbon feed stream through a hydroprocessing vessel. Liquid quenches (from high pressure hot separator) were installed to assist in cooling the reactor inter-bed, and to maintain good liquid irrigation of the catalyst. The soluble hydrogen in the stream, kinetically active and available for immediate reaction, is the final piece of the puzzle for why this unit runs so well.

Abstract: A process and apparatus are disclosed for hydrocracking hydrocarbon feed in a hydrocracking unit and hydrotreating a diesel product from the hydrocracking unit in a hydrotreating unit. The hydrocracking unit and the hydrotreating unit share the same recycle gas compressor. A make-up hydrogen stream may also be compressed in the recycle gas compressor. A warm separator separates recycle gas and hydrocarbons from diesel in the hydrotreating effluent, so fraction of the diesel is relatively simple. The warm separator also keeps the diesel product separate from the more sulfurous diesel in the hydrocracking effluent, and still retains heat needed for fractionation of lighter components from the low sulfur diesel product.

Abstract: A process and system are described for the processing of gas associated with crude oil production, i.e. associated gas. A separation complex is used to separate produced fluids produced from a hydrocarbon reservoir into crude oil, liquefied petroleum gas, water, and natural gas. At least a portion of the natural gas is converted into synthesis gas in a synthesis gas generator. A combination of a synthesis gas conversion catalysts and hydroconversion catalysts are used in a synthesis gas reactor to convert the synthesis gas into a liquid effluent stream containing liquefied petroleum gas and a synthetic crude oil. The liquefied petroleum gas and synthetic crude oil from the synthesis gas reactor is sent to the separation complex. Liquefied petroleum gas is separated both from the synthetic crude oil and a natural crude oil obtained from the produced fluids.

Abstract: Provided is a method of manufacturing diesel fuel, including: fractionating in a first fractionator a synthetic oil obtained by Fisher-Tropsch synthesis into at least two fractions of a middle fraction, and a wax fraction containing a wax component heavier than the middle fraction; hydroisomerizing the middle fraction by bringing the middle fraction into contact with a hydroisomerizing catalyst to produce a hydroisomerized middle fraction; hydrocracking the wax fraction by bringing the wax fraction into contact with a hydrocracking catalyst to produce a wax decomposition compound; fractionating in a second fractionator a mixture of the hydroisomerized middle fraction and the hydrocracked wax fraction into at least two fractions including a kerosene fraction and a gas oil fraction; and mixing the at least two fractions at a predetermined blend ratio to produce a diesel fuel having a kinematic viscosity at 30° C. of 2.5 mm2/s or more and a pour point of ?7.5° C. or less.

Abstract: Non-hydrotreated biocomponent feeds can be mixed with mineral feeds and processed under catalytic isomerization/dewaxing conditions. The catalytic isomerization/dewaxing conditions can be selected to advantageously also substantially deoxygenate the mixed feed. Diesel fuel products with improved cold flow properties can be produced.

Abstract: Integrated isomerization and ionic liquid catalyzed alkylation processes may comprise integrating ionic liquid alkylation and n-butane isomerization using a common distillation unit for separating an n-butane containing fraction from at least one of an alkylation hydrocarbon phase from an ionic liquid alkylation reactor and an isomerization hydrocarbon stream from an isomerization unit. The n-butane containing fraction may undergo isomerization to provide an isomerization reactor effluent comprising the isomerization hydrocarbon stream. An isobutane containing fraction, separated from at least one of the alkylation hydrocarbon phase and the isomerization hydrocarbon stream, may be recycled from the distillation unit to the ionic liquid alkylation reactor.

Abstract: A process for the hydroprocessing of a low value light cycle oil (LCO) hydrocarbon feed to provide a high-value diesel-range product. The process comprises a hydrotreatment stage followed by a hydrocracking stage, each of which is conducted under liquid-full reaction conditions wherein substantially all the hydrogen supplied to the hydrotreating and hydrocracking reactions is dissolved in the liquid-phase hydrocarbon feed. Ammonia and other gases formed during hydrotreatment are removed in a separation step prior to hydrocracking. The LCO feed is advantageously converted to diesel in high yield with little loss of hydrocarbon to naphtha.

Abstract: A process for the hydroprocessing of a low value light cycle oil (LCO) hydrocarbon feed to provide a high-value diesel-range product. The process comprises a hydrotreatment stage followed by a hydrocracking stage, each of which is conducted under liquid-full reaction conditions wherein substantially all the hydrogen supplied to the hydrotreating and hydrocracking reactions is dissolved in the liquid-phase hydrocarbon feed. Ammonia and other gases formed during hydrotreatment are removed in a separation step prior to hydrocracking. The LCO feed is advantageously converted to diesel in high yield with little loss of hydrocarbon to naphtha.

Abstract: An apparatus and process is disclosed for hydroprocessing hydrocarbon feed in a hydroprocessing unit and hydrotreating a second hydrocarbon. A warm separator sends vaporous hydrotreating effluent to be flashed with liquid hydroprocessing effluent to produce a vapor flash overhead that can be recycled to the hydrotreating unit to provide hydrogen requirements.

Abstract: A quenching medium is delivered directly to selected regions or locations within a catalyst bed in a hydroprocessing reactor vessel in order to control the reactivity of a hydroprocess occurring in the selected regions or locations separately from other regions or locations. Temperature sensors for providing temperature indications and conduits for delivering the quench medium are distributed throughout the catalyst bed. One or more conduits can be selected for delivery of the quenching medium to selected regions or locations so that separate control of the level of reactivity in each of various regions or locations throughout the bed can be achieved.

Abstract: The present invention relates to a method of preparing synthetic crude oil from a heavy crude reservoir, comprising: (a) extracting the heavy crude oil using a steam technology; (b) separating the crude extracted and the water; (c) separating the crude into at least one light cut and one heavy cut; (d) converting said heavy cut to a lighter product and a residue; (e) optionally, partially or totally hydroprocessing the converted product and/or the light cut(s) obtained upon separation (c); (f) burning and/or gasifying the conversion residue in the presence of metal oxides in at least one chemical looping cycle producing CO2-concentrated fumes in order to allow CO2 capture, the optionally hydroprocessed converted product and light separation cut(s) making up the synthetic crude oil, said combustion allowing to generate steam and/or electricity, and said gasification allowing to generate hydrogen, the steam and/or the electricity thus generated being used for extraction (a), and/or the electricity and/or the hy

Abstract: The present invention relates to a process for regeneration of alkali metal salt reagent used in desulfurization of heavy oil feedstreams. In particular, the present invention relates to a process utilizing potassium hydroxide as an external supply reagent to a heavy oil conversion process and in-situ conversion of the spent reactants utilized in such process into a potassium sulfide reagent for reintroduction into the heavy oil conversion process.

Abstract: Feeds containing a hydrotreated biocomponent portion, and optionally a mineral portion, can be processed under catalytic conditions for isomerization and/or dewaxing. The sulfur content of the feed for dewaxing can be selected based on the hydrogenation metal used for the catalyst. Diesel fuel products with improved cold flow properties can be produced.

Abstract: A process is disclosed for converting distillate to gasoline-range hydrocarbons using a two-stage catalyst system including a first catalyst containing a Group VIII metal and a zeolite, and a second catalyst containing a Group VIII metal, tin and an inorganic oxide support.

Abstract: A process for maximizing p-xylene production begins by producing a naphtha fraction and a light cycle oil fraction from a fluid catalytic cracking zone. The gasoline and light cycle oil fractions are combined and hydrotreated to produce a hydrotreated product. Fractionation of the hydrotreated product in a fractionation zone makes a light ends cut, a naphtha cut, a hydrocracker feed and an unconverted oil fraction. The hydrocracker feed is sent to a hydrocracking zone to make a hydrocracker product, which is then recycled back to the fractionation zone, feeding the hydrocracker product above an outlet for the hydrocracker feed, but below an outlet for the naphtha cut. The naphtha cut goes to a dehydrogenation zone where hydrogen is removed to make aromatics from naphthenes to make a dehydrogenated naphtha. The dehydrogenated naphtha is fed to an aromatics recovery unit to recover p-xylene and other aromatics.

Abstract: A reforming process includes integrating catalytic cracking product naphtha dehydrogenation and naphtha from a hydrocracking zone and feeding them to a dehydrogenation zone. The dehydrogenation zone includes a first portion of reforming catalyst from a catalyst regenerator that moves downward through the dehydrogenation zone. A product stream from the dehydrogenation zone flows to an aromatics unit and is separated into an aromatic-rich extract and a raffinate. Straight run naphtha and the raffinate are introduced to a first reforming zone that includes a second portion of reforming catalyst. The reforming catalyst moves through the first reforming zone then is removed from the bottom of each of the first reforming zone and the dehydrogenation zone and is fed to a second reforming zone. An effluent from the first reforming zone is fed to a plurality of reforming zones. The reforming catalyst moves downward through the multiple reforming zones then to a regenerator.

Abstract: A divided wall column can allow for fractionation of multiple streams while maintaining separate product qualities. Effluents from multiple stages of a reaction system can be processed in a single divided wall column. The divided wall column can produce multiple cuts from each separated area, as well as at least one output from a common area. At least one reaction stage can advantageously have a continuous liquid phase environment.

Abstract: This invention relates to a process for electrochemical conversion of dibenzothiophene type molecules of petroleum feedstreams selectively to mercaptan compounds that can then be more easily removed from the electrochemically treated product stream by either caustic extraction or thermal decomposition of the thiol functionality to hydrogen sulfide. The conversion of dibenzothiophenes to mercaptans is performed by electrochemical means in the substantial absence of hydrogen and in the substantial absence of water.

Abstract: This invention describes a two-stage regeneration zone that has a regenerated catalyst circuit such as the one that results from the mixing of a partially regenerated catalyst with a residual coke rate of between 0.3 and 0.7% and a totally regenerated catalyst with a coke rate that is less than 0.15%. All things being equal, this double-population regenerated catalyst enables the maximization of the LCO yield.

Abstract: Systems and methods for hydroprocessing a heavy oil feedstock are disclosed. The system employs a plurality of contacting zones and at least one separation zone, wherein a solvating hydrocarbon having a normal boiling point less than 538° C. (1000° F.) is employed. In the system, a mixture of heavy oil feedstock and solvating hydrocarbon is provided to a contact zone along with a slurry catalyst feed in a hydrocarbon diluent. The contacting zone operates at a temperature and pressure near the critical temperature and pressure of the heavy oil and solvating hydrocarbon mixture to convert at least a portion of the heavy oil feedstock to lower boiling hydrocarbons, forming upgraded products.

Abstract: The present invention describes a process for the production of gasoline in a fluid catalytic cracking unit having at least one principal reactor operating using feeds with a low Conradson Carbon and a high hydrogen content, said process comprising recycling a coking cut either to a side chamber branching off the stripper or within the stripper itself by means of a tubular vessel within said stripper.

Abstract: The invention relates to a method for the catalytic hydrotreatment of a load based on a diesel fuel oil and a biological load based on plant oils and/or animal fats in a hydrotreatment unit. The invention is characterized in that the hydrotreatment unit comprises at least one hydrotreatment reactor operating on a countercurrent. The invention also relates to a hydrotreatment unit for implementing said method, and a corresponding hydrorefining unit.

Abstract: A process is provided that is directed to a steam pyrolysis zone integrated with a solvent deasphalting zone and a hydrotreating zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics.

Abstract: A process is provided that is directed to a steam pyrolysis zone integrated with a hydroprocessing zone including residual bypass to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics.

Abstract: An integrated hydrotreating and steam pyrolysis process for the direct processing of a crude oil is provided to produce olefinic and aromatic petrochemicals. Crude oil and hydrogen are charged to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity. Hydroprocessed effluent is thermally cracked in the presence of steam to produce a mixed product stream, which is separated. Hydrogen from the mixed product stream is purified and recycled to the hydroprocessing zone, and olefins and aromatics are recovered from the separated mixed product stream.

Abstract: Steam pyrolysis and hydroprocessing are integrated including hydrogen redistribution to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. A feed is initially split into a light portion and a heavy portion, and the heavy portion is hydroprocessed. A hydroprocessed effluent is charged, along with steam, to a convection section of a steam pyrolysis zone. The mixture is heated and passed to a vapor-liquid separation section. A residual portion is removed and light components are charged to a pyrolysis section of the steam pyrolysis zone. A mixed product stream is recovered from the steam pyrolysis zone and it is separated into product including olefins and aromatics.

Abstract: In a process for producing synthetic fuels from an educt mixture containing hydrogen and oxygenates, such as methanol and/or dimethyl ether, the educt mixture is reacted on a catalyst in a first process stage to obtain a hydrocarbon product containing olefins with preferably 2 to 8 carbon atoms. In a second process stage the hydrocarbon product is oligomerized to long-chain olefins, from which gasoline and Diesel products are obtained. The hydrocarbon product obtained in the first process stage is separated into a liquid phase and a gaseous phase. The gaseous phase is supplied to the second process stage. The liquid phase is separated into a mixture rich in C6? hydrocarbons and a mixture containing C7+ hydrocarbons and aromatics. The mixture rich in C6? hydrocarbons is supplied to the second process stage. The mixture containing C7+ hydrocarbons ?+ and aromatics can be admixed to the gasoline product for quality improvement.

Abstract: A process for maximizing p-xylene production includes producing a naphtha fraction and a light cycle oil fraction from a fluid catalytic cracking zone. These fractions are combined and hydrotreated. Fractionation of the hydrotreated product makes a hydrocracker feed that is sent to a hydrocracking zone to make a naphtha cut and a hydrocracker product. The hydrocracker product is recycled back to the fractionation zone, and the naphtha cut is dehydrogenated in a dehydrogenation zone to make aromatics. Reforming catalyst from a catalyst regenerator moves downward through the dehydrogenation zone. Straight run naphtha and raffinate from the aromatics unit are introduced to an additional series of reforming zones. The reforming catalyst moves in parallel through the first reforming zone and the dehydrogenation zones, then is combined for entry to the second and subsequent reforming zones prior to regeneration.

Abstract: The present invention describes a reaction zone comprising at least two fluidized reactors, a principal reactor for cracking a heavy hydrocarbon cut, the other, additional, reactor for cracking one or more light cuts, the effluents from the two reactors being treated in a common gas-solid separation and quench zone. Performance is enhanced because the thermal degradation reactions in the reaction zone are controlled in an optimum manner.

Abstract: An apparatus and process is disclosed for hydroprocessing hydrocarbon feed in a hydroprocessing unit and hydrotreating a second hydrocarbon. The hydrotreating effluent is mixed with hydroprocessing effluent and together fractionated.

Abstract: Process for the production of high-quality kerosene and diesel fuels and for the coproduction of hydrogen from a so-called light naphtha cut to which any quantity of LPG cut can be added where the steps of the process include: separating normal and iso-paraffins, dehydrogenation of the paraffins, oligomerization of the olefins and hydrogenation of the oligomerized olefins, the process permitting the production of kerosene and diesel fuels meeting market specifications, or even improved relative to the latter.

Abstract: A method for preparing the low carbon number petrochemical products along with the high energy fuels from pyrolysis gasoline is provided. In this method, the pyrolysis gasoline is used as feedstock, and the reactive non-aromatic, unsaturated moieties, and the sulfur impurity contained in the pyrolysis gasoline are removed. Then the stabilized feedstock is used to produce C5 olefins, C6-C9 aromatic hydrocarbons as petrochemical products, and C10+ hydrocarbons as precursors of high energy fuels. Upon acid catalytic isomerization, or upon crystallization followed by acid catalytic isomerization, the C10+ hydrocarbons as precursors of high energy fuels are converted to exo-isomers as high energy fuels.

Abstract: Disclosed herein are methods of manufacturing renewable chemicals through the manufacture of novel triglyceride oils followed by chemical modification of the oils. Methods such as transesterification, hydrogenation, hydrocracking, deoxygenation, isomerization, interesterification, hydroxylation, hydrolysis and saponification are disclosed. Novel oils containing fatty acid chain lengths of C8, C10, C12 or C14 are also disclosed and are useful as feedstocks in the methods of the invention.

Abstract: Systems and methods for hydroprocessing heavy oil feedstock is disclosed. The process employs a plurality of contacting zones and at least a separation zone to convert at least a portion of the heavy oil feedstock to lower boiling hydrocarbons, forming upgraded products. In one embodiment, water and/or steam being injected into at least a contacting zone. The contacting zones operate under hydrocracking conditions, employing at least a slurry catalyst. In one embodiment, at least a portion of the non-volatile fractions recovered from at least one of the separation zones is recycled back to at least a contacting zone (“recycled mode”). In one embodiment, the number of separation zones is less than the number of contacting zones in the system. In the separation zones, upgraded products are removed overhead and optionally treated in an in-line hydrotreater; and the bottom stream is optionally further treated in a fractionator.

Abstract: A process for refining or pre-refining a crude oil P is described in which P is fractionated into several fractions, wherein partial oxidation of an asphaltenic residue R1 derived from P is carried out to produce a synthesis gas SG1 with an H2/CO ratio of less than 1, steam cracking is carried out of an external light hydrocarbon fraction to produce a synthesis gas SG2 with a H2/CO ratio of more than 3; SG1 and SG2 are mixed to produce a synthesis gas SG with a H2/CO ratio in the range 1.2 to 2.5, and SG is converted by Fischer-Tropsch synthesis, then the waxes produced are converted into middle distillates. Preferably, a vacuum distillate VGO and/or a deasphalted oil DAO derived from P are hydrocracked mixed with the waxes. The invention also pertains to a facility for carrying out the process.

Abstract: The invention provides for a process for dewaxing a waxy hydrocarbon feedstock to form a lubricant oil. The invention is also directed to a catalyst system comprising a hydrotreating catalyst upstream of a dewaxing catalyst, used in the dewaxing of a waxy hydrocarbon feedstock to form a lubricant oil. In particular, the invention is directed to a process and catalyst system designed to maintain yield of lubricant oil product. Specifically, the yield of lubricant oil does not decrease more than 2%, at a target pour point, over a dewaxing temperature range. The hydrotreating catalyst helps prevent aging of the dewaxing catalyst and maintains lubricant oil product yield at a target pour point over a wide temperature range. The hydrotreating catalyst comprises platinum, palladium, or combinations thereof on a low acidity inorganic oxide support where acidity is measured by a decalin conversion of less than 10% at 700° F.

Abstract: Multiple catalytic processing stations enable a method for producing volatile gas streams from biomass decomposition at discrete increasing temperatures. These catalytic processing stations can be programmed to maximize conversion of biomass to useful renewable fuel components based on input feedstock and desired outputs.