Abstract: A hydrocracking process for maximization of naphtha while producing base oil is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking unit in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream, a diesel stream and a first unconverted oil stream. A recycle stream comprising a portion of the kerosene stream, a portion of the diesel stream, and a portion of the first unconverted oil stream is recycled to the hydrocracking unit to provide a second unconverted oil stream. A remaining portion of the first unconverted oil stream is withdrawn for base oil production.

Abstract: Systems and methods include an aromatics complex (ARC), the ARC in fluid communication with a naphtha reforming unit (NREF) and operable to receive a reformate stream produced by the NREF, and the ARC further operable to separate the reformate stream into a gasoline pool stream, an aromatics stream, and an aromatic bottoms stream; and a hydrodearylation unit operable to receive heavy, non-condensed, alkyl-bridged, multi-aromatic compounds from the aromatic bottoms stream, the hydrodearylation unit further operable to hydrogenate and hydrocrack the heavy, non-condensed, alkyl-bridged, multi-aromatic compounds to produce a stream suitable for recycle to the NREF or the reformate stream, where the hydrodearylation unit is further operable to receive hydrogen produced in the NREF.

Abstract: Systems and methods include an aromatics complex (ARC), the ARC in fluid communication with a naphtha reforming unit (NREF) and operable to receive a reformate stream produced by the NREF, and the ARC further operable to separate the reformate stream into a gasoline pool stream, an aromatics stream, and an aromatic bottoms stream; and a hydrodearylation unit operable to receive heavy, non-condensed, alkyl-bridged, multi-aromatic compounds from the aromatic bottoms stream, the hydrodearylation unit further operable to hydrogenate and hydrocrack the heavy, non-condensed, alkyl-bridged, multi-aromatic compounds to produce a stream suitable for recycle to the NREF or the reformate stream, where the hydrodearylation unit is further operable to receive hydrogen produced in the NREF.

Abstract: The present invention relates to a process for preparing a difunctional catalyst using a zeolite IZM-2, a hydrogenating function and a matrix. The preparation process according to the invention simultaneously allows preferential localization of said hydrogenating function on the surface and/or in the microporosity of zeolite IZM-2 and homogeneous distribution of the hydrogenating function in the catalyst and preferably on zeolite IZM-2 by means of using an impregnation solution comprising specific noble metal precursors combined with the presence of ammonium salts, with a quite precise ratio of ammonium salt to noble metal.

Abstract: Provided here are systems and methods that integrate a hydrodearylation process and a transalkylation process into an aromatic recovery complex. Various other embodiments may be disclosed and claimed.

Abstract: Methods and apparatus for recovering power in a hydroprocessing process are described. The method involves the use of a power-recovery turbine in place of, or in addition to, a control valve. A hydrocarbon feed stream is combined with a portion of a hydrogen stream. The combined stream is heated, and the heated stream is introduced into a hydroprocessing reaction zone having at least two beds. The heated stream is contacted with a first hydroprocessing catalyst to form a first hydroprocessed stream. At least part of a portion of the hydrogen stream is combined with the first hydroprocessed stream to form a first quenched hydroprocessed stream. The first quenched hydroprocessed stream is contacted with a second hydroprocessing catalyst to form a second hydroprocessed stream. At least a portion of the second portion of the hydrogen stream is directed through a power-recovery turbine to generate electric power.

Abstract: Systems and methods are provided for catalytic hydroprocessing to form lubricant base oils. The methods can include performing high pressure hydrofinishing after fractionating the hydrotreated and/or hydrocracked and/or dewaxed effluent. Performing hydrofinishing after fractionation can allow the high hydrogen pressure for hydrofinishing to be used on one or more lubricant base oil fractions that are desirable for high pressure hydrofinishing. This can allow for improved aromatic saturation of a lubricant base oil product while reducing or minimizing the hydrogen consumption. The high pressure hydrofinishing can be performed at a hydrogen partial pressure of at least about 2500 psig (˜17.2 Mpa), or at least about 2600 psig (˜18.0 Mpa), or at least about 3000 psig (˜20.6 MPa). The high pressure hydrofinishing can allow for formation of a lubricant base oil product with a reduced or minimized aromatics content, a reduced or minimized 3-ring aromatics content, or a combination thereof.

Abstract: Systems and processes for the production of fuel and fuel blends involve the production of fuels for blending with one or more alcohols such as ethanol and/or butanol. A method for producing a fuel blend includes blending a light distillate product from an oil refinery with butanol. The fuel blending can be at the oil refinery.

Abstract: A process and apparatus is for recycling LCO and/or HCO to an FCC unit to recover additional distillate. Spent catalyst recycle in the FCC unit may be used to improve distillate yield. A hydroprocessing zone may saturate cycle oil aromatics for cracking in an FCC unit. The recycle cracked stream may be recycled to a downstream hydroprocessing zone to avoid a first hydroprocessing zone for hydrotreating feed to the FCC unit. Additional recovery of cycle oil for recycle is obtained by heating slurry oil prior to vacuum separation.

Abstract: Embodiments of the present disclosure include methods for producing aromatic products, the methods including separating a crude oil and condensate feed into at least a light naphtha stream, a heavy naphtha stream, and a bottoms stream, reforming at least a portion of the heavy naphtha stream to produce a reformate stream, feeding a cracker feed stream, comprising the light naphtha stream, the bottoms stream, and a reformate extraction raffinate, to an olefins cracker to produce cracker products comprising pyrolysis gasoline, and introducing an extractor feed stream comprising the pyrolysis gasoline and the reformate to an aromatic extraction unit to produce an aromatic product and the reformate extraction raffinate.

Abstract: A process and apparatus for recovering cycle oil from FCC CSO is described. By feeding the additional cycle oil to a hydrocracking unit additional diesel, naphtha and petrochemical feedstock may be obtained. The additional cycle oil is obtained by vacuum separation of the CSO. The described process and apparatus can provide additional recovery for a refiner.

Abstract: A process for selectively dealkylating aromatic compounds includes providing a coal tar stream comprising aromatic compounds and hydrotreating the coal tar stream to reduce a concentration of one or more of organic sulfur, nitrogen, and oxygen in the coal tar stream, and to hydrogenate at least a portion of the aromatic compounds in the coal tar stream. The process further includes hydrocracking the hydrotreated coal tar stream to further hydrogenate the aromatic compounds and to crack at least one ring of multi-ring aromatic compounds to form single-ring aromatic compounds. The single-ring aromatic compounds present in the hydrocracked stream are then dealkylated to remove alkyl groups containing two or more carbon atoms.

Abstract: A process and apparatus for recycling LCO and/or HCO to a hydroprocessing zone to saturate aromatics for cracking in an FCC unit is disclosed. The recycle cracked stream may be recycled to a downstream hydroprocessing zone to avoid a first hydroprocessing zone that is primarily for demetallizing (and desulfurizing) feed to the FCC unit.

Abstract: A method of processing a coal feed to produce aromatic hydrocarbon compounds includes providing a coal tar stream and converting the coal tar stream to a conversion product comprising at least olefins, paraffins, and aromatics. The process further includes separating the olefins and C5? paraffins from the conversion product, and contacting the separated olefins and the C5? paraffins with a catalyst to dehydrogenize, oligomerize, and cyclize the olefins and the C5? paraffins, to form aromatic hydrocarbon compounds.

Abstract: A reforming process using a medium pore zeolite under conditions to facilitate the conversion of C8 paraffinic compounds to para-xylene is provided. Para-xylene is produced at greater than thermodynamic equilibrium concentrations using the process.

Abstract: A process for selectively dealkylating aromatic compounds includes providing a coal tar stream comprising aromatic compounds and hydrotreating the coal tar stream to reduce a concentration of one or more of organic sulfur, nitrogen, and oxygen in the coal tar stream, and to hydrogenate at least a portion of the aromatic compounds in the coal tar stream. The process further includes hydrocracking the hydrotreated coal tar stream to further hydrogenate the aromatic compounds and to crack at least one ring of multi-ring aromatic compounds to form single-ring aromatic compounds. The single-ring aromatic compounds present in the hydrocracked stream are then dealkylated to remove alkyl groups containing two or more carbon atoms.

Abstract: A method of processing a coal feed to produce aromatic hydrocarbon compounds includes providing a coal tar stream and converting the coal tar stream to a conversion product comprising at least olefins, paraffins, and aromatics. The process further includes separating the olefins and C5? paraffins from the conversion product, and contacting the separated olefins and the C5? paraffins with a catalyst to dehydrogenize, oligomerize, and cyclize the olefins and the C5? paraffins, to form aromatic hydrocarbon compounds.

Abstract: A coal tar process is described. A coal tar stream is provided, and the coal tar stream is separated to provide a plurality of hydrocarbon streams. At least one of the hydrocarbon streams is hydroprocessed in a fluidized bed hydroprocessing zone with a catalyst to provide a gaseous volatile product and a solid heavy hydrocarbon product absorbed onto the catalyst. The gaseous volatile product is separated from the catalyst. The catalyst is regenerating by separating the absorbed heavy hydrocarbon product from the catalyst. The regenerated catalyst is recycled into the hydroprocessing zone.

Abstract: The present invention is directed to the modification of the hydrocarbon production sequence of operations including the Fischer-Tropsch process for the production of hydrocarbon fuels in an efficient manner, along with the production of commercially valuable co-products from by-products of the hydrocarbon production process.

Abstract: A process is provided for producing a heavy lubricating base oil by hydrocracking a lubricating oil feedstock at high yield. The lubricating oil feedstock contains a hydroprocessed stream that is difficult to process using a conventional catalyst system. The catalyst used in the process includes a mixed metal sulfide catalyst that comprises at least one Group VIB metal and at least one Group VIII metal. The process also provides for hydroisomerization and hydrofinishing process steps to prepare the lubricating base oil.

Abstract: There is provided a method for dewaxing a hydrocarbon oil for improving the life of a hydroisomerization catalyst. An aspect of a method for dewaxing a hydrocarbon oil according to the present invention comprises: a first step of subjecting a hydrocarbon oil in which a peroxide value is 100 ppm by mass or more to hydrotreating to obtain a material to be treated in which a peroxide value is 30 ppm by mass or less; and a second step of subjecting the material to be treated in which a peroxide value is 30 ppm by mass or less to hydroisomerization treatment using a hydroisomerization catalyst.

Abstract: A process is disclosed for hydrocracking a primary hydrocarbon feed and a diesel co-feed in a hydrocracking unit and hydrotreating a diesel product from the hydrocracking unit in a hydrotreating unit. The diesel stream fed through the hydrocracking unit is pretreated to reduce sulfur and ammonia and can be upgraded with noble metal catalyst.

Abstract: The present disclosure is directed to processes using a new crystalline molecular sieve designated SSZ-96, which is synthesized using a 1-butyl-1-methyl-octahydroindolium cation as a structure directing agent.

Abstract: A method for producing a lubricant base oil, the method comprising a first step of fractionating, from a hydrocarbon oil containing a base oil fraction and a heavy fraction that is heavier than the base oil fraction, the base oil fraction and the heavy fraction, and a second step of obtaining a dewaxed oil by isomerization and dewaxing of the base oil fraction fractionated in the first step, wherein a hydrocracked oil obtained by hydrocracking the heavy fraction fractionated in the first step is returned to the first step.

Abstract: A lubricant base oil that is a hydrocarbon oil having a kinematic viscosity at 100° C. of 2.0 to 9 mm2/s, a viscosity index of 130 or more, a freezing point of ?30 to ?5° C., and an SBV viscosity at ?20° C. of 1,000 to 60,000 mPa·s, in which the freezing point of the lubricant base oil is higher by 10° C. or more than a freezing point of raffinate obtained by bringing the lubricant base oil into contact with urea and removing paraffin that can be included in the urea.

Abstract: A lubricant base oil that is a hydrocarbon oil that satisfies any of the following conditions (i), (ii) and (iii): (i) a hydrocarbon oil having a kinematic viscosity at 100° C. of 3.0 to 5.0 mm2/s, a viscosity index of 145 or more, and an SBV viscosity at ?20° C. of 3,000 to 60,000 mPa·s, (ii) a hydrocarbon oil having a kinematic viscosity at 100° C. of 5 to 9 mm2/s, a viscosity index of 155 or more, and an SBV viscosity at ?20° C. of 3,000 to 30,000 mPa·s, and (iii) a hydrocarbon oil having a kinematic viscosity at 100° C. of 2.0 to 3.0 mm2/s, a viscosity index of 130 or more, and an SBV viscosity at ?30° C. of 1,000 to 30,000 mPa·s.

Abstract: Disclosed is a method of manufacturing high quality lube base oil (Group III) from unconverted oil having various properties obtained in a variety of hydrocrackers using improved catalytic dewaxing and hydrofinishing, the method including producing unconverted oil of at least one kind in the same or different hydrocrackers; subjecting the unconverted oil to vacuum distillation; supplying all or part of the distillate fractions to a catalytic dewaxing reactor; supplying the dewaxed oil fraction to a hydrofinishing reactor; and stripping the hydrofinished light oil fraction, wherein make-up hydrogen is supplied upstream of the hydrofinishing reactor to increase hydrogen partial pressure, thereby enabling high quality base oil to be manufactured at high yield under optimal process conditions using unconverted oil produced by hydrocracking under various conditions.

Abstract: This invention discloses a process for making high viscosity index lubricating base oils having a viscosity index of at least 110 by co-feeding a ketone or a beta-keto-ester feedstock with a lubricant oil feedstock directly to a hydrocracking unit to produce a hydrocracked stream. Then at least a portion of the hydrocracked stream is treated under hydroisomerization conditions to produce a high viscosity index lubricating base oil. The process may involve bypassing a hydrotreating or hydrofinishing step, which may result in improved efficiency and economics in producing high viscosity index lubricating base oils.

Abstract: In a hydrocarbon upgrading process, a hydrocarbon feed is treated in at least one of a steam cracker, catalytic cracker, coker, hydrocracker, and reformer under suitable conditions to produce a first stream comprising olefinic and aromatic hydrocarbons. A second stream composed mainly of C4 to C12+ olefinic and aromatic hydrocarbons is recovered from the first stream and blended said second stream with a residual fraction from a steam cracker or an atmospheric or vacuum distillation unit to produce a third stream. The third stream is then catalytically pyrolyzed in a reactor under conditions effective to produce a fourth stream having an increased benzene and/or toluene content compared with said second stream and a C3-olefin by-product. The C3-olefin by-product is recovered and benzene and/or toluene are recovered from the fourth stream.

Abstract: The present invention provides a method for producing a gas oil composition which contains a cracked base gas oil with a poor oxidation stability but is enhanced in oxidation stability resulting in less sludge or deposit formation. The method comprises blending 0.5 to 15 percent by volume of a cracked reformed base oil having a total aromatic content of 80 to 100 percent by volume, a bicyclic aromatic content of 40 to 95 percent by volume, a 10 vol. % distillation temperature of 160 to 250° C. and a 90 vol. % distillation temperature of 260 to 330° C. and 10 to 70 percent by volume of a cracked base gas oil thereby producing a gas oil composition with an induction period of 60 minutes or longer, a sulfur content of 10 ppm by mass or less and a cetane number of 45 or greater.

Abstract: A biocomponent feedstock can be hydroprocessed using a hydrogen-containing refinery as a source of hydrogen gas. A relatively low cost catalyst, such as a water gas shift catalyst and/or spent hydrotreating catalyst, can be used as a hydrogenation catalyst for the process. The hydroprocessing can allow for olefin saturation and/or deoxygenation of the biocomponent feed by using a relatively low value refinery stream, e.g., containing from about 20 mol % to about 60 mol % hydrogen.

Abstract: This invention relates to a process for conducting a hydrocracking or a hydrotreating process in a microchannel reactor. This invention also relates to a process and apparatus for flowing a vapor and liquid into a plurality of microchannels in a microchannel processing unit.

Abstract: The invention relates to a process for the production of middle distillates from a paraffinic feedstock that is produced by Fischer-Tropsch synthesis, implementing a hydrocracking/hydroisomerization catalyst that comprises at least one hydro-dehydrogenating metal that is selected from the group that is formed by the metals of group VIB and group VIII of the periodic table and a substrate that comprises at least one zeolite that has at least one series of channels of which the opening is defined by a ring with 12 oxygen atoms modified by a) a stage for introducing at least one alkaline cation that belongs to group IA or IIA of the periodic table, b) a stage for treatment of said zeolite in the presence of at least one molecular compound that contains at least one silicon atom, c) at least one stage for partial exchange of said alkaline cations by NH4+ cations such that the remaining content of alkaline cations in the modified zeolite at the end of stage c) is such that the alkaline cation/aluminum molar ratio

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: Methods and systems for idling a hydrocracker are provided. The method can include hydrocracking a hydrocarbon in the presence of a catalyst and hydrogen in a reactor to produce a hydrocracked product. A kill agent can be introduced to the reactor in an amount sufficient to reduce hydrocracking by at least 10% therein. In some examples, the kill agent can include one or more nitrogen-containing compounds, such as ammonia, amines, anilines, ammonia-containing compounds, amine-containing compounds, or, aniline-containing compounds. In some examples, the catalyst can include one or more Group VIII metals (e.g., cobalt, nickel, palladium, iron, alloys thereof), one or more Group VIB metals (e.g., molybdenum, tungsten, alloys thereof, or oxides thereof), and a catalyst support, such as a zeolite.

Abstract: A process for upgrading residuum hydrocarbons is disclosed. The process may include: contacting a residuum hydrocarbon fraction and hydrogen with a first hydroconversion catalyst in a first ebullated bed hydroconversion reactor system; recovering a first effluent from the first ebullated bed hydroconversion reactor system; solvent deasphalting a vacuum residuum fraction to produce a deasphalted oil fraction and an asphalt fraction; contacting the deasphalted oil fraction and hydrogen with a second hydroconversion catalyst in a second hydroconversion reactor system; recovering a second effluent from the second hydroconversion reactor system; and fractionating the first effluent from the first ebullated bed hydroconversion reactor system and the second effluent from the second hydroconversion reactor system to recover one or more hydrocarbon fractions and the vacuum residuum fraction in a common fractionation system.

Abstract: A hydrocarbon conversion catalyst composition which comprises dealuminated ZSM-48 and/or EU-2 zeolite and a refractory oxide binder essentially free of alumina, processes for preparing such composition and processes for converting hydrocarbon feedstock with the help of such compositions.

Abstract: We provide a process to manufacture a base stock, comprising hydrocracking, separating, and dewaxing, wherein the base stock has a ratio of Noack volatility to CCS VIS at ?25° C. multiplied by 100 from 0.15 to 0.40. We also provide a base stock made by a process, and a base oil manufacturing plant that produces the base stock.

Abstract: Process for the hydroconversion of heavy oils, selected from crude oils, heavy crude oils, bitumens from tar sands, distillation residues, distillation heavy cuts, distillation deasphalted residues, vegetable oils, oils from coal and oil shale, oils from the thermodecomposition of waste material, polymers, biomasses, comprising sending the heavy oil to a hydroconversion area, effected in one or more ebullated bed reactors, wherein hydrogen is introduced, in the presence of a suitable heterogeneous, supported, hydroconversion catalyst, in addition to a suitable hydrogenation catalyst, nano-dispersed in said heavy oil, and sending the stream coming from the hydroconversion area to a separation area, in which the separated liquid fraction, containing the nano-dispersed catalyst, is recycled to the ebullated bed reactor(s).

Abstract: A process is 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 shares the same 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: The invention concerns integration of hydroprocessing and steam cracking. A feed comprising crude or resid-containing fraction thereof is severely hydrotreated and passed to a steam cracker to obtain an olefins product.

Abstract: Disclosed is a method of manufacturing high-quality naphthenic base oil by subjecting, as a feedstock, light cycle oil (LCO) and slurry oil (SLO) obtained through fluidized catalytic cracking (FCC) to hydrotreating and dewaxing.

Abstract: The invention provides a process for converting a paraffinic feedstock comprising at least 50 wt % of compounds boiling above 370° C., a paraffin content of at least 60 wt %, an aromatics content below 1 wt %, a naphthenic content below 2 wt %, a nitrogen content below 0.1 wt %, and a sulphur content below 0.1 wt %, comprising: (a) reacting the feedstock with hydrogen at a temperature between 175 and 400° C. and a pressure between 20 and 100 bar using a catalyst comprising 0.005 to 5.0 wt % of a Group VIII noble metal on a carrier comprising 0.1-15 wt % zeolite beta and at least 40 wt % amorphous silica-alumina (b) withdrawing the effluent (c) subjecting the effluent to a fractionation step to form a heavy fraction, an intermediate fraction, and a light fraction; and (d) providing at least part of the heavy fraction to the reaction zone.

Abstract: A process is described for the production of middle distillates from a paraffinic feedstock wherein the feedstock is subjected to hydrocracking and/or hydro-isomerization in the presence of a hydrocracking/hydro-isomerization catalyst. The catalyst comprises at least one hydro-dehydrogenating metal selected from metals of groups VIB and VIII, and a substrate that comprises at least one dealuminified Y zeolite. The dealuminified Y zeolite is modified by a basic treatment stage wherein the dealuminified Y zeolite is mixed with a basic aqueous solution, and at least one heat treatment stage.

Abstract: A suitable feedstock for forming lubricant base oils is separated into at least a lower boiling portion and a higher boiling portion. The lower boiling portion is combined with a feed suitable for use as a fuels hydrocracking feed. The combined feed is hydrocracked and catalytically dewaxed in order to form fuels and Group II, Group II+, or Group III light neutral basestocks. The higher boiling portion of the feedstock is solvent processed in order to form Group I heavy neutral base oils and/or Group I brightstock base oils. The higher boiling portion of the feedstock can correspond to both a bottoms fraction and one or more additional fractions boiling above a fractionation cut point.

Abstract: Described herein is a hydrocracking and/or hydrotreatment process which uses a catalyst comprising an active phase containing at least one hydrogenating/dehydrogenating component, and a support comprising at least one dealuminated zeolite Y having an overall initial atomic ratio of silicon to aluminum between 2.5 and 20, an initial weight fraction of extra-lattice aluminum atoms greater than 10%, an initial mesopore volume greater than 0.07 ml.g?1, and an initial crystal lattice parameter a0 between 24.38 ? and 24.30 ?. The zeolite Y is modified by a basic treatment stage, and at least one thermal treatment stage.

Abstract: Process for hydrotreating a heavy hydrocarbon fraction using a system of switchable fixed bed guard zones each containing at least two catalyst beds and in which whenever the catalyst bed that is brought initially into contact with the feed is deactivated and/or clogged during the steps in which the feed passes successively through all the guard zones, the point of introduction of the feed is shifted downstream. The present invention also relates to an installation for implementing this process.

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: The present invention relates to a method of hydro-upgrading inferior gasoline through ultra-deep desulfurization and octane number recovery. The method comprises the following steps: cutting inferior full-range gasoline into light fraction gasoline and heavy fraction gasolines; contacting the light fraction gasoline successively with a catalyst for selective diene removal and a catalyst for desulfurization and hydrocarbon multi-branched-chain hydroisomerization; contacting the heavy fraction gasoline with the catalyst for selective hydrodesulfurization in a first reactor, and contacting the reaction effluent from the first reactor with a catalyst for supplemental desulfurization and hydrocarbon aromatization/single-branched-chain hydroisomerization in a second reactor; and blending the treated light fraction gasoline and the heavy fraction gasoline to obtain the ultra-clean gasoline product.