Abstract: The invention concerns a process for producing middle distillates from a paraffinic feed produced by Fischer-Tropsch synthesis, using a hydrocracking/hydroisomerization catalyst which comprises 0.2% to 2.5% by weight of an oxide of a doping element selected from boron, phosphorus, silicon, at least one hydrodehydrogenating element selected from the group formed by noble elements from group VIII of the periodic table, a non-zeolitic support based on silica-alumina containing more than 5% by weight and 95% by weight or less of silica (SiO2), specifically defined pore characteristics, a BET specific surface area in the range 100 to 550 m2/g, and with an X ray diffraction diagram which contains at least the characteristic principal peaks of at least one of the transition aluminas included in the group composed of alpha, rho, khi, eta, gamma, kappa, theta and delta aluminas.

Abstract: Contact of a crude feed with one or more catalysts produces a total product that includes a crude product. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed. The one or more catalysts may include at least one catalyst having a median pore diameter of at least 230 ?. Methods for producing the catalyst having the median pore size diameter are described.

Abstract: ITQ-34 (INSTITUTO DE TECNOLOGÍA QUÍMICA number 34) is a new crystalline microporous material with a framework of tetrahedral atoms connected by atoms capable of bridging the tetrahedral atoms, the tetrahedral atom framework being defined by the interconnections between the tetrahedrally coordinated atoms in its framework. ITQ-34 can be prepared in silicate compositions with an organic structure directing agent. It has a unique X-ray diffraction pattern, which identifies it as a new material. ITQ-34 is stable to calcination in air, absorbs hydrocarbons, and is catalytically active for hydrocarbon conversion.

Abstract: Contact of a crude feed that has a viscosity of at least 10 cSt at 37.8° C. (100° F.) and an API gravity of at least 10 with one or more catalysts produces a total product that includes a crude product. The crude product is a liquid mixture at 25° C. and 0.101 MPa. The crude product has a viscosity of at most 90% of the viscosity of the crude feed and an API gravity of about 70% to about 130% of the API gravity of the crude feed. In some instances, one or more other properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Abstract: The present invention relates to a microporous crystalline material characterized in that it has the following chemical composition in the calcined from: xX2O3:nYO2:mGeO2 in which (n+m) is at least 5, X is one or more trivalent elements, Y corresponds to one or more tetravalent elements other than Ge, “x” may have any value, including zero, and the ratio Y/Ge is greater than 0.1, and it has a characteristic X-ray diffraction pattern. Its also relates to a method for preparing it and to its use in the conversion of organic-compounds supplies.

Abstract: The present invention concerns doped catalysts on a mixed zeolite/alumino-silicate support with a low macropore content, and hydrocracking/hydroconversion and hydrotreatment processes employing them. The catalyst comprises at least one hydrodehydrogenating element selected from the group formed by elements from group VIB and group VIII of the periodic table and a doping element in a controlled quantity selected from phosphorus, boron and silicon, and a support based on zeolite Y defined by a lattice parameter a of the unit cell in the range 24.40×10?10 m to 24.15×10?10 m and silica-alumina containing a quantity of more than 5% by weight and 95% by weight or less of silica (SiO2).

Abstract: Contact of a crude feed with one or more catalysts produces a total product that include a crude product. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more other properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Abstract: The present invention describes a hydrocracking and/or hydrotreatment process using a catalyst comprising an active phase containing at least one hydrogenating/dehydrogenating component selected from the group VIB elements and the non-precious elements of group VIII of the periodic table, used alone or in a mixture, and a support comprising at least one dealuminated zeolite Y having an overall initial atomic ratio of silicon to aluminium between 2.5 and 20, an initial weight fraction of extra-lattice aluminium atoms greater than 10%, relative to the total weight of aluminium present in the zeolite, an initial mesopore volume measured by nitrogen porosimetry greater than 0.07 ml·g?1 and an initial crystal lattice parameter a0 between 24.38 ? and 24.30 ?, said zeolite being modified by a) a stage of basic treatment comprising mixing said dealuminated zeolite Y with a basic aqueous solution, and at least one stage c) of thermal treatment.

Abstract: The invention relates to a method for synthesizing a hydroprocessing catalyst, wherein the support is prepared by mixing peptized aluminium with amorphous silica or with crystalline aluminium silicate as a catalyst component. The catalyst comprises a metal from group VIB and/or a metal from group VIIIB of the Periodic Table. The catalyst exhibits enhanced activity vis-à-vis hydrodisintegration, hydrodemetallization and hydrodesulphurization, and has a relatively stable life as a function of run time. Thus, the invention relates to a method for developing a catalyst for hydroprocessing heavy hydrocarbon feedstocks, which is characterized in that it comprises two steps: the first step involves optimization of the catalyst formulation with respect to textural properties, the number of acid sites and incorporation of the active metal; the second step involves evaluation with real feedstocks and the stability of the catalyst as is function of run time.

Abstract: The present invention describes a method for hydrocracking and/or hydrotreating hydrocarbon-containing feeds using a catalyst comprising at least one hydro-dehydrogenizing metal selected from the group made up of group VIB and non-noble group VIII metals of the periodic table and a support comprising at least one zeolite having at least pore openings containing 12 oxygen atoms, modified by a) at least a stage of introducing at least one alkaline cation belonging to groups IA or IIA of the periodic table, b) a stage of treating said zeolite in the presence of at least one molecular compound containing at least one silicon atom, c) at least one stage of partial exchange of said alkaline cations by NH4+ cations in such a way that the proportion of alkaline cations remaining in the modified zeolite at the end of stage c) is such that the alkaline cation/aluminium molar ratio ranges between 0.2:1 and 0.01:1, and d) at least one thermal treatment stage.

Abstract: The present invention pertains to a process for hydroprocessing a heavy hydrocarbon oil, comprising contacting a heavy hydrocarbon oil in the presence of hydrogen with a mixture of hydroprocessing catalyst I and hydroprocessing catalyst II. The process of the invention combines high contaminant removal with high conversion, low sediment formation, and high process flexibility.

Abstract: Methods and systems for contacting of a crude feed with one or more catalysts to produce a total product that includes a crude product are described. The crude product is a liquid mixture at 25° C. and 0.101 MPa. The crude product has an MCR content of at most 90% of the MCR content of the crude feed. One or more other properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Abstract: The present invention concerns doped catalysts on an alumino-silicate support with an adapted macropore content and hydrocracking/hydroconversion and hydrotreatment processes employing them. The catalyst comprises at least one hydrodehydrogenating element selected from the group formed by elements from group VIB and group VIII of the periodic table, a controlled quantity of phosphorus (optionally in combination with boron and/or silicon) as a doping element, and a non-zeolitic support based on alumina-silica containing a quantity of more than 5% by weight and 95% by weight or less of silica (SiO2).

Abstract: A method for obtaining jet fuel from diesel fuel is provided, the method comprising subjecting the diesel fuel to hydrocracking to convert at least a portion of the diesel fuel into a mixture of light hydrocarbons, kerosene, naphtha and a liquefied petroleum gas, isolating the kerosene, recovering jet fuel from the kerosene, subjecting at least a portion of the mixture of kerosene, naphtha and a liquefied petroleum gas to steam forming to obtain a synthesis gas containing hydrogen, and recycling hydrogen contained in the synthesis gas to the hydrocracking step. A modular system for performing the method is also provided.

Abstract: Contact of a crude feed with one or more catalysts produces a total product that include a crude product. The crude feed has a total content of alkali metal, and alkaline-earth metal, in metal salts of organic acids of at least 0.00001 grams per gram of crude feed. At least one of the catalysts includes vanadium. The crude product is a liquid mixture at 25° C. and 0.101 MPa and has a total content of alkali metal, and alkaline-earth metal, in metal salts of organic acids of at most 90% of the total content of alkali metal, and alkaline-earth metal, in metal salts of organic acids of the crude feed. One or more other properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Abstract: A catalyst and process for hydrotreating and/or hydroconverting heavy metal-containing hydrocarbon feeds, said catalyst comprising a support in the form of beads based on alumina, at least one catalytic metal or a compound of a catalytic metal from group VIB (column 6 in the new periodic table notation), optionally at least one catalytic metal or compound of a catalytic metal from group VIII (columns 8, 9 and 10 of the new periodic table notation), with a pore structure composed of a plurality of juxtaposed agglomerates, each formed by a plurality of acicular platelets, the platelets of each agglomerate being generally radially orientated with respect to each other and with respect to the center of the agglomerate. The catalyst also comprises at least one doping element selected from the group constituted by phosphorus, boron, silicon (or silica which does not belong to that which could be contained in the selected support) and halogens.

Abstract: The invention relates to a catalyst including at least one hydro-dehydrogenating element chosen from the group formed by the group VIB and group VIII elements of the periodic table and a substrate based on a silica-alumina matrix with a reduced content of macropores containing a quantity greater than 5% by weight and less than or equal to 95% by weight of silica (SiO2) and based on at least one zeolite. The invention also relates to a substrate based on a silica-alumina matrix with a reduced content of macropores containing a quantity greater than 5% by weight and less than or equal to 95% by weight of silica (SiO2) and based on at least one zeolite. The invention also relates to hydrocracking and/or hydroconversion processes and hydrotreating processes utilizing a catalyst according to the invention.

Abstract: A process for hydrocracking a hydrocarbon feedstock comprising components boiling above 343° C. into a middle distillate fraction in the presence of hydrogen under hydrocracking conditions, comprising contacting the hydrocarbon feedstock in a first hydrocracking zone in the presence of one or more hydrocracking catalysts and thereafter in a second hydrocracking zone in the presence of one or more hydrocracking catalysts, and recovering a middle distillate product, wherein the entire effluent from the first hydrocracking zone is passed into the second hydrocracking zone, and at least one hydrocracking catalyst in the first hydrocracking zone comprises one or more hydrogenation components on a support comprising at least one large pore zeolite having a pore diameter in the range of 0.7-1.

Abstract: The invention relates to a process for FCC pretreatment by mild hydrocracking of a hydrocarbon feedstock that comprises a vacuum distillate fraction or a deasphalted oil or else a mixture of these two fractions, said primary feedstock, to produce gas oil and an effluent having an initial boiling point of more than 320° C., said effluent (FCC feedstock) then being subjected to a catalytic cracking, process in which at least 85% by weight of said primary feedstock ends above 375° C. and at least 95% by weight of said primary feedstock ends below 650° C., whereby the mild hydrocracking is performed under an absolute pressure of 2 to 12 MPa and at a temperature of between 300 and 500° C., characterized in that the hydrocarbon feedstock also comprises a lighter hydrocarbon fraction, a so-called secondary feedstock, of which at least 50% by weight ends below 375° C. and at least 80% ends above 200° C.

Abstract: A method for preparation of ethylene and propylene by catalytic cracking using a fluid-bed catalyst. The main technical problems to be solved are a relatively high reaction temperature, and low activities and poor selectivities of the catalyst at a low temperature, during the reaction for preparing ethylene and propylene by catalytically cracking naphtha. The fluid-bed catalyst is a composition of the chemical formula Mo1.0VaAbBcCdOx based on stoichiometric ratio. The method using the fluid-bed catalyst has satisfactorily solved the above-mentioned problems, and is useful in the industrial production of ethylene and propylene by catalytically cracking naphtha.

Abstract: Compositions for reduction of NOx generated during a catalytic cracking process, preferably, a fluid catalytic cracking process, are disclosed. The compositions comprise a fluid catalytic cracking catalyst composition, preferably containing a Y-type zeolite, and a particulate NOx composition containing particles of a zeolite having a pore size ranging from about 3 to about 7.2 Angstroms and a SiO2 to Al2O3 molar ratio of less than about 500. Preferably, the NOx reduction composition contains NOx reduction zeolite particles bound with an inorganic binder. In the alternative, the NOx reduction zeolite particles are incorporated into the cracking catalyst as an integral component of the catalyst. Compositions in accordance with the invention are very effective for the reduction of NOx emissions released from the regenerator of a fluid catalytic cracking unit operating under FCC process conditions without a substantial change in conversion or yield of cracked products.

Abstract: A method for producing an LPG fraction, a gasoline fraction, a kerosene fraction, a gas oil fraction, monocyclic aromatic hydrocarbon and a non-aromatic naphtha fraction from hydrocracked oil includes hydrocracking hydrocarbon oil containing polycyclic aromatic hydrocarbon to convert into a light hydrocarbon fraction, and efficiently and selectively producing monocyclic aromatic hydrocarbon with higher valuable alkylbenzenes. The method for producing hydrocarbon fraction comprises subjecting hydrocarbon feedstock containing polycyclic aromatic hydrocarbon and in which the ratio of carbons constituting an aromatic ring to the total carbons in the hydrocarbon oil (the aromatic ring-constituting carbon ratio) is 35 mole % or more to catalytic cracking in the presence of hydrogen. 40% or more of a fraction with a boiling point of 215° C. or higher in the hydrocarbon feedstock is converted into a fraction with a boiling point lower than 215° C.

Abstract: The present invention relates to a catalyst composition for the reaction of hydrocarbons comprising a zeolite with has a faujasite structure and a fibrous zeolite which comprises essentially non-crossing one-dimensional channels. Further, the catalyst composition comprises in a preferred embodiment a metal component selected from metals of the group VIB and VIII of the periodic table of elements and their compounds. The invention relates further to a process for the synthesis of such a catalyst composition and to a process for hydrocracking hydrocarbon feedstocks by using said catalyst composition.

Abstract: Contact of a crude feed with one or more catalysts produces a total product that includes a crude product. The crude feed may include Micro-Carbon Residue (MCR), oxygen, sulfur, or mixtures thereof. The crude product is a liquid mixture at 25° C. and 0.101 MPa. The crude product may have a MCR residue and/or oxygen content of at most 90% of the MCR residue content and/or oxygen content of the crude feed. In some instances, the crude product may have a sulfur content of about 30% to about 70% of the sulfur content of the crude feed. One or more other properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Abstract: Bulk bi-metallic catalysts for use in the hydroprocessing of hydrocarbon feeds, as well as a method for preparing such catalysts. The catalysts are prepared from a catalyst precursor containing an organic agent.

Abstract: Increased yields of middle distillate and jet fuel and increased catalyst activity are obtained in a hydrocracking process by the use of a catalyst containing a beta zeolite and a Y zeolite having a unit cell size from 24.37 to 24.43 angstrom. The catalyst has a relatively high amount of Y zeolite relative to beta zeolite.

Abstract: The present invention concerns doped catalysts on an alumino-silicate support with an adapted macropore content and hydrocracking/hydroconversion and hydrotreatment processes employing them. The catalyst comprises at least one hydrodehydrogenating element selected from the group formed by elements from group VIB and group VIII of the periodic table, a controlled quantity of phosphorus (optionally in combination with boron and/or silicon) as a doping element, and a non-zeolitic support based on alumina-silica containing a quantity of more than 5% by weight and 95% by weight or less of silica (SiO2).

Abstract: Aspects of the invention include methods to produce jet-fuel from biological oil sources. The method may be comprised of two steps: a hydrocracking and a reforming. The process may be self sufficient in heat and hydrogen.

Abstract: A method is disclosed for hydroprocessing a heavy hydrocarbon oil, comprising a first hydroprocessing step of bringing a heavy hydrocarbon oil into contact with a Catalyst (1) with a certain specific surface area and pore size distribution in the presence of hydrogen in a first reaction zone containing the Catalyst (1), and a second hydroprocessing step of bringing the hydroprocessed oil obtained from the first reaction zone into contact with a Catalyst (2) with a certain specific surface area and pore size distribution in the presence of hydrogen in a second reaction zone containing the Catalyst (2). The method is an improvement in decreasing or inhibiting the sediment formation, while highly hydroprocessing a heavy hydrocarbon oil containing a large amount of impurities such as sulfur, micro carbon residue (MCR), metals, nitrogen and asphaltene, especially a heavy oil containing a large amount of heavy vacuum residue, to adequately remove the impurities.

Abstract: Increased yields of LPG and middle distillate products are obtained in a two stage hydrocracking process by the use of a catalyst containing a beta zeolite. In embodiments, the beta zeolite has not been hydrothermally treated or has been hydrothermally treated at a relatively low temperature. In another embodiment, the catalyst contains a relatively low amount of beta zeolite.

Abstract: A hydrogenation catalyst for a hydrocarbon oil, includes an inorganic porous support composed of at least the oxides of aluminum, phosphorus, and silicon, and supporting at least one active metal selected from the metals of Group 8 of the periodic table, at least one active metal selected from the metals of Group 6 of the periodic table, and phosphorus, the phosphorus chemical shift value of the inorganic support determined by 31P-CPMAS-NMR having the peak within the range of 0 to ?20 ppm. The catalyst can achieve an extremely high level of hydrogenation wherein the hydrocarbon is decreased in sulfur content to 10 ppm by mass or less and in nitrogen content to 3 ppm by mass or less.

Abstract: Process for transforming a gas-oil fraction that makes it possible to produce a fuel that has a quality according to stringent requirements in terms of sulfur content, aromatic compound content, cetane number, boiling point, T95, of 95% of the compounds and density, d15/4, at 15° C. This process comprises a hydrorefining stage and a hydrocracking stage, whereby the latter uses a catalyst that contains at least one zeolite. The conversion of products that have a boiling point of less than 150° C. is, throughout the two stages of hydrocracking and hydrorefining, less than 40% by weight and, for the hydrorefining stage, between 1 and 15% by weight. The temperature, TR2, of the hydrocracking stage is less than the temperature, TR1, of the hydrorefining stage, and the variation between temperatures TR1 and TR2 is between 0 and 80° C.

Abstract: Process for transforming a gas oil fraction that makes it possible to produce a fuel that has a quality according to stringent requirements in terms of sulfur content, aromatic compound content, cetane number, boiling point, T95, of 95% of the compounds and density, d15/4, at 15° C. This process comprises a hydrorefining stage and a subsequent stage, whereby the latter uses a catalyst that is selected from the group that consists of hydrorefining catalysts and catalysts that comprise at least one mixed oxide, a metal of group VIB, and a non-noble metal of group VIII. The conversion of products that have a boiling point of less than 150° C. is, for the hydrorefining stage, between 1 and 15% by weight. The temperature, TR2, of the subsequent stage is less than the temperature, TR1, of the hydrorefining stage, and the variation between temperatures TR1 and TR2 is between 0 and 80° C.

Abstract: An amorphous support, methods for making the same and methods of using, particularly in hydrocracking. A method of making may comprise mixing a first amorphous material and a second amorphous material of different acidities to form a mixture, and treating by either separately treating the first and second amorphous materials before mixing or treating the mixture, so as to form an amorphous catalyst support. Treating preferably includes calcining. The acidity of the amorphous support may be modified by the different acidities of the precursor amorphous materials, their proportions in the mixture, and/or the order of the mixing and treating steps. A method of use may comprise reacting a hydrocarbon fraction with hydrogen over a hydrocracking catalyst comprising the amorphous catalyst support to form a hydrocracked product. Further embodiments include the first and second amorphous materials comprising silica-alumina, and/or differing in Brönsted acidity, Lewis acidity, or acidity index.

Abstract: Hydrocarbon fluids are produced by hydrocracking a vacuum gas oil stream, fractionating and/or hydrogenating the hydrocracked vacuum gas oil. The fluids typically have ASTM D86 boiling point ranges within the range 100° C. to 400° C. the range being no more than 75° C., they also have a naphthenic content greater than 60%, the naphthenics containing polycyclic materials, an aromatic content below 2% and an aniline point below 100° C. The fluids are particularly useful as solvents, for printing inks, drilling fluids, metal working fluids and as silicone extenders.

Abstract: This invention relates to silico-aluminum substrates, catalysts, and the hydrocracking and hydrotreatment processes that use them. The catalyst comprises at least one hydro-dehydrogenating element that is selected from the group that is formed by elements of group VIB and group VIII of the periodic table and a non-zeolitic silica-alumina-based substrate that contains an amount of more than 5% by weight and less than or equal to 95% by weight of silica (SiO2) and has the following characteristics: A mean pore diameter, measured by mercury porosimetry, encompassed between 20 and 140 ?, a total pore volume, measured by mercury porosimetry, encompassed between 0.1 ml/g and 0.6 ml/g, a total pore volume, measured by nitrogen porosimetry, encompassed between 0.1 ml/g and 0.6 ml/g, a BET specific surface area encompassed between 100 and 550 m2/g, a pore volume, measured by mercury porosimetry, encompassed in the pores with diameters of more than 140 ?, of less than 0.

Abstract: The instant invention is directed to a process for upgrading heavy oils using a slurry composition. The slurry composition is prepared in a series of steps, involving mixing a Group VIB metal oxide with aqueous ammonia to form an aqueous mixture and sulfiding the mixture to form a slurry. The slurry is then promoted with a Group VIII metal compound. Subsequent steps involve mixing the slurry with a hydrocarbon oil, and combining the resulting mixture with hydrogen gas (under conditions which maintain the water in a liquid phase) to produce the active slurry catalyst.

Abstract: Hydrocracking catalyst composition comprising an optional metal hydrogenation component supported on a carrier comprising a zeolite of the faujasite structure having a unit cell size in the range of from 24.10 to 24.40 ?, a bulk silica to alumina ratio (SAR) above about 12, and a surface area of at least about 850 m2/g as measured by the BET method and ATSM D4365-95 with nitrogen adsorption at a p/po value of 0.03.

Abstract: The present invention pertains to a catalyst comprising 7–20 wt. % of a Group VIB metal component, calculated as trioxide on the weight of the catalyst, and 0.5 to 6 wt. % of a Group VIII metal component, calculated as oxide on the weight of the catalyst, on a porous inorganic carrier. The catalyst has a specific surface area of 100–180 m2/g, a total pore volume of at least 0.55 ml/g, at least 50% of the total pore volume in pores with a diameter of at least 20 nm (200 ?), 10–30% of the total pore volume in pores with a diameter of at least 200 nm (2000 ?), and 0–1% of the total pore volume in pores with a diameter above 1000 nm (10000 ?). The catalyst is particularly suitable for the hydroprocessing of heavy hydrocarbon feeds of which at least 50 wt. % boils above 538° C. (1000° F.). It is especially advantageous for the hydroprocessing of feedstocks of which at least 80 wt. % boils above 538° C. (1000° F.).

Abstract: A catalyst contains at least one group VIII element and at least molybdenum and/or tungsten, said elements being present at least in part in the catalyst in the dry state in the form of at least one heteropolyanion with formula MxAB6O24H6C(3-2x), tH2O; MxAB6O24H6C(4-2x), tH2O; MxA2B10O38H4C(6-2x), tH2O; MxA2B10O38H4C(8-2x), tH2O; or MxA2B10O38H4C(7-2x), tH2O, in which M is cobalt and/or nickel and/or iron and/or copper and/or zinc, A is one or two elements from group VIII of the periodic table, B is molybdenum and/or tungsten and C is an H+ ion and/or a (NR1R2R3R4)+ type ammonium ion, in which R1, R2, R3 and R4, which may be identical or different, correspond either to a hydrogen atom or to an alkyl group and/or caesium and/or potassium and/or sodium, t is a number between 0 and 15 and x takes a value in the range 0 to 4 depending on the formula.

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: Increased yields of middle distillate products are obtained in a hydrocracking process by the use of a catalyst containing a Beta zeolite which has been hydrothermally treated to adjust the distribution of relatively weak and strong acid sites. The number of strong acid sites is reduced, preferably by steaming at a temperature above 750° C. for at least one hour, with the acidity distribution being measured by pyridine IR adsorption values taken at 150° C., and 300° C., and 450° C.

Abstract: A catalyst composition comprising a minor amount of a low acidity, highly dealuminated ultra stable Y zeolite having an Alpha value of less than about 5, preferable less than about 3 and Broensted acidity measured by FT-IR from about 1 to about 20, preferably from about 1-10, micro mole/g of, a homogeneous, amorphous silica-alumina cracking component having an SB ratio of from about 0.7 to about 1.3, wherein a crystalline alumina phase is present in an amount of no greater than about 10%, preferably no greater than 5% and a catalytic amount of hydrogenation component selected from the group consisting of a Group VI metal, a Group VIII metal, and mixtures thereof is disclosed. The present invention provides for a process for converting hydrocarbonaceous oils comprising contacting the hydrocarbonaceous oils with the catalyst under suitable hydrocarbon conversion conditions.

Abstract: The invention pertains to a hydroprocessing catalyst comprising a Group VIB hydrogenation metal component, a non-noble Group VIII hydrogenation metal component, an alkali metal component, and silica. The catalyst has a specific surface area, total pore volume and pore size distribution. The invention also pertains to the use of this catalyst in hydroprocessing of heavy hydrocarbon feedstocks, e.g, in an ebullated bed process.

Abstract: The present invention pertains to a process for the hydroprocessing of hydrocarbon feedstocks wherein said hydrocarbon feedstocks are contacted, at hydroprocessing conditions, with a catalyst composition comprising at least one Group VIII non-noble metal component and at least two Group VIB metal components. The catalyst composition further comprises at least about 0.01 mole of an organic oxygen-containing additive per mole of the total of Group VIB metals and Group VIII non-noble metals present in the catalyst composition. The total of the Group VIII and Group VIB metal components, calculated as oxides, make up at least about 50 wt. % of the catalyst composition, calculated on dry weight.

Abstract: A catalyst composition comprising a low acidity, highly dealuminated ultra stable Y zeolite having an Alpha value of less than about 3 and Broensted acidity measured by FT-IR from about 1 to about 20, preferably from about 1-10, micro mole/g of, an amorphous cracking component and a catalytic amount of hydrogenation component selected from the group consisting of a Group VI metal, a Group VIII metal, and mixtures thereof is disclosed. The present invention provides for a process for converting hydrocarbonaceous oils comprising contacting the hydrocarbonaceous oils with the catalyst under suitable hydrocarbon conversion conditions. Such processes in include, but are not limited to, single stage hydrocracking, two-stage hydrocracking, series-flow hydrocracking, mild hydrocracking, lube hydrocracking, hydrotreating, lube hydrofinishing, hydrodesulphurization, hydrodenitrification, catalytic dewaxing and catalytic cracking.

Abstract: A catalytic hydrocracking process wherein a hydrocarbonaceous feedstock and a liquid recycle stream is contacted with hydrogen in a hydrocracking reaction zone at elevated temperature and pressure to obtain conversion to lower boiling hydrocarbons. A liquid hydrocarbonaceous stream produced from the effluent of the hydrocracking reaction zone is fractionated in a first zone of a divided-wall fractionation zone to produce at least one liquid hydrocarbonaceous product stream and a liquid hydrocarbonaceous stream containing hydrocarbons boiling at a temperature in the boiling range of the feedstock and heavy polynuclear aromatic compounds. At least a portion of the liquid hydrocarbonaceous stream containing heavy polynuclear aromatic compounds is introduced into a second zone of the divided-wall fractionation zone to produce a stream rich in polynuclear aromatic compounds.

Abstract: A process to produce base oils through the use of fractionation, solvent extraction, dewaxing, and hydrofinishing

Abstract: The present invention pertains to a catalyst comprising 7-20 wt. % of a Group VIB metal component, calculated as trioxide on the weight of the catalyst, and 0.5 to 6 wt. % of a Group VIII metal component, calculated as oxide on the weight of the catalyst, on a porous inorganic carrier. The catalyst has a specific surface area of 100-180 m2/g, a total pore volume of at least 0.55 ml/g, at least 50% of the total pore volume in pores with a diameter of at least 20 nm (200 Π), 10-30% of the total pore volume in pores with a diameter of at least 200 nm (2000 Π), and 0-1% of the total pore volume in pores with a diameter above 1000 nm (10000 Π). The catalyst is particularly suitable for the hydroprocessing of heavy hydrocarbon feeds of which at least 50 wt. % boils above 538° C. (1000° F.). It is especially advantageous for the hydroprocessing of feedstocks of which at least 80 wt. % boils above 538° C. (1000° F.).

Abstract: A hydrocracking catalyst containing at least one matrix, at least one zeolite chosen from the group formed by the zeolites ZBM-30, ZSM-48, EU-2, and EU-11, at least one Y zeolite, at least one hydro-dehydrogenating metal chosen from the group formed by the metals from Group VIB and Group VIII of the periodic table, optionally at least one element chosen from the group formed by phosphorus, boron and silicon, optionally at least one element from Group VIIA, and optionally at least one element from Group VIIB is used in a process of hydrocracking/hydroconversion of hydrocarbon charges.