СПОСОБ ГИДРОПЕРЕРАБОТКИ УГЛЕВОДОРОДНОГО СЫРЬЯ

Изобретение относится к усовершенствованному способу гидропереработки углеводородного сырья, содержащего серу- и/или азотсодержащие загрязняющие вещества. Указанный способ включает первое контактное взаимодействие углеводородного сырья с водородом в присутствии, по меньшей мере, одного первого катализатора на основе металлов VIII группы на кислотном носителе, причем носитель выбирают из группы цеолитов и цеолитсодержащих носителей, а затем поток, выходящий с первого катализатора, непосредственно контактирует с водородом в присутствии, по меньшей мере, одного второго катализатора на основе металла VIII группы на менее кислотном твердом носителе, причем указанный твердый носитель выбирают из группы носителей на основе диоксида кремния-оксида алюминия и других твердых носителей, не являющихся цеолитами. При указанной комбинации двух слоев катализатора появляется возможность перерабатывать сырье с высоким содержанием загрязняющих примесей без высокого уровня крекинга, связанного с использованием ...

СПОСОБ ГИДРИРОВАНИЯ СИНТЕТИЧЕСКОЙ НЕФТИ И СПОСОБ ИЗГОТОВЛЕНИЯ БАЗОВОГО ТОПЛИВА

Изобретение относится к способу гидроочистки синтетической нефти, осуществляемому контактированием синтетической нефти, полученной посредством синтеза Фишера-Тропша и имеющей содержание углеводородов С9-21 90 массовых % или более, с катализатором гидроочистки, который представляет собой катализатор, который содержит носитель, содержащий одну или более твердых кислот, выбранных из сверхстабильного Y-(USY) цеолита, алюмосиликатного, циркониевосиликатного и алюмоборного окисного катализатора, и по меньшей мере один металл, выбранный из группы, состоящей из металлов, принадлежащих к группе VIII Периодической Таблицы, нанесенный на носитель, в присутствии водорода с регулированием температуры реакции при контактировании катализатора гидроочистки с синтетической нефтью, для гидроочистки синтетической нефти таким образом, что содержание (массовые %) С8 и более низких углеводородов в синтетической нефти после контакта составляет на 3-9 массовых % больше, чем перед контактом. Изобретение также касается ...

СПОСОБ ПОЛУЧЕНИЯ БАЗОВОГО СМАЗОЧНОГО МАСЛА ИЗ ПАРАФИНОВОГО ГАЧА

Использование: нефтеперерабатывающая отрасль промышленности. Сущность: сырье, содержащее парафиновый гач, подвергают контактированию в присутствии водорода с сульфидированным катализатором гидрообессеривания, содержащим никель и вольфрам на кислотном и имеющим активность гидрообессеривания выше 30%. Далее проводят стадию снижения температуры застывания потока, выходящего со стадии контактирования. Технический результат: повышение качества целевого продукта. 23 з.п. ф-лы.

СПОСОБ ПАССИВАЦИИ АЗОТОСОДЕРЖАЩИМ СОЕДИНЕНИЕМ ЦЕОЛИТНОГО КАТАЛИЗАТОРА, В ЧАСТНОСТИ КАТАЛИЗАТОРА ГИДРОКРЕКИНГА

Изобретение касается способа обработки ex-situ катализатора, содержащего, по меньшей мере, одну гидрирующую фазу и, по меньшей мере, один аморфный алюмосиликат или цеолит, содержащий кислотные центры. Способ включает: стадию введения азота контактированием при температуре меньше 100°С с по меньшей мере одним азотсодержащим соединением основного характера, которое представляет собой аммиак или соединение, разлагающееся с образованием аммиака, при этом указанное соединение вводят из расчета от 0,5 до 10% (в расчете на массу N), и стадию сульфирования/активации газом, содержащим водород и сероводород, при температуре, по меньшей мере, 250°С, причем эту стадию осуществляют перед стадией введения указанного азотсодержащего соединения, и полученный катализатор, возможно, сушат. Эта обработка дает возможность быстрого запуска, эффективного на установке гидрокрекинга. 2 н. и 12 з.п. ф-лы, 1 табл., 4 пр.

ГИДРОПЕРЕРАБОТКА УГЛЕВОДОРОДНОГО СЫРЬЯ

... 1. Способ гидропереработки углеводородного сырья, содержащего серу- и/или азотсодержащие загрязняющие вещества, указанный способ включает первое контактное взаимодействие углеводородного сырья с водородом в присутствии, по меньшей мере, одного первого катализатора на основе металлов VIII группы на кислотном носителе, причем носитель выбирают из группы цеолитов и цеолитсодержащих носителей, а затем контактное взаимодействие сырья с водородом в присутствии, по меньшей мере, одного второго катализатора на основе металла VIII группы на менее кислотном твердом носителе, причем указанный твердый носитель выбирают из группы носителей на основе диоксида кремния-оксида алюминия и других твердых носителей, не являющихся цеолитами. 2. Способ по п.1, в котором указанная гидропереработка включает гидроконверсию, гидрокрекинг, гидрообработку, гидрирование, гидроочистку и гидроизомеризацию нефтяных типов сырья, таких как растворители и средний дистиллят. 3. Способ по п.1 или 2, в котором твердый носитель ...

Способ получения особо чистых насыщенных углеводородов C-C

FIELD: chemistry. SUBSTANCE: invention relates to organic chemistry and specifically to the technology of cleaning and drying liquefied hydrocarbon gases, particularly for producing coolants, and can be used in gas and chemical industry. Described is a method of producing especially pure saturated hydrocarbons C 3 -C 4 , such as especially pure propane or especially pure isobutane, which includes preliminary purification of technical liquefied hydrocarbon gas, such as propane, isobutane, n-butane, from mercaptans in adsorber, subsequent purification of liquefied hydrocarbon gas from unsaturated hydrocarbons C 3 -C 4 in chemical reactor, purification of liquefied hydrocarbon gas from hydrocarbon and air impurities in rectification unit and drying of end product, wherein during preliminary cleaning from mercaptans using adsorber with diameter of 500–900 mm, filled with adsorbent with layer height of 900 mm, wherein liquefied hydrocarbon gas is fed into adsorber at a rate providing contact time of 0.5–6.0 hours at temperature of minus 20 °C – plus 30 °C and pressure of 0.1–1.6 MPa, wherein the adsorbent used is silica gel impregnated with a saturated solution of copper (II) sulphate or chloride, further purification from unsaturated hydrocarbons C 3 -C 4 liquefied hydrocarbon gas in amount of 300–500 kg is carried out in a chemical reactor with a hydrogenation catalyst loaded therein in amount of 5 kg, at temperature of minus 20 °C – plus 30 °C and pressure of 0.3–1.6 MPa, wherein hydrogen is fed into reactor in amount of 0.6–1.0 m 3 and hydrogenation catalyst used is aluminosilicate with palladium applied in amount of 0.5 wt%, and purification from hydrocarbon and air impurities is carried out by periodic rectification under pressure corresponding to pressure of hydrocarbon gas at temperature of 35–40 °C, in equipped with tanks for fraction collection to rectification unit, consisting of cube with capacity of 1.6 m 3 , columns with height of 4 m and diameter of 0.2 m, ...

СПОСОБ ГИДРООБРАБОТКИ НЕФТЯНЫХ ФРАКЦИЙ

... 1. Способ гидрообработки нефтяных фракций, включающий контакт нефтяных фракций с катализатором, содержащим гидрид металла типа внедрения, имеющим реакционную поверхность и одноатомный водород на реакционной поверхности, причем гидрид металла типа внедрения представляет собой гидрид сплава, содержащего металл VIII группы и лантанид или металл II группы. ! 2. Способ по п.1, в котором гидрид металла типа внедрения содержит накапливающие водород междоузлия, которые способны высвобождать одноатомный водород. ! 3. Способ по п.1, в котором гидрид металла типа внедрения содержит частицы, имеющие диаметр от примерно 0,01 до примерно 1000 мкм. ! 4. Способ по п.1, в котором реакционная поверхность, по существу, свободна от оксидного слоя. ! 5. Способ по п.1, дополнительно включающий подачу газообразного молекулярного водорода при контакте нефтяных фракций с катализатором, содержащим гидрид металла типа внедрения. ! 6. Способ по п.5, в котором накапливающие водород междоузлия одновременно повторно ...

ШАРИКОВЫЙ КАТАЛИЗАТОР ДЛЯ ГИДРООЧИСТКИ НЕФТЯНЫХ ФРАКЦИЙ И СПОСОБ ЕГО ПРИГОТОВЛЕНИЯ

... 1. Шариковый катализатор для гидроочистки нефтяных фракций, состоящий из носителя - оксида алюминия, активных компонентов - соединений молибдена, никеля или кобальта в виде оксидов и/или сульфидов и, возможно, дополнительно цеолита Y в водородной форме, представляющий собой гранулы сферической или эллиптической формы, отличающийся тем, что гранулы катализатора имеют насыпную плотность от 0,40 до 0,50 г/мл и объемом пор не менее 1,2 мл/г.2. Способ приготовления катализатора для гидроочистки нефтяных фракций по п.1, состоящего из носителя - оксида алюминия и активных компонентов - соединений молибдена, никеля или кобальта и возможно цеолита Y в водородной форме, включающий пептизацию исходного порошка источника оксида алюминия водным раствором органической кислоты с получением псевдозоля, формовку в растворе аммиака, сушку и прокаливание носителя с последующем введением в него активных компонентов и, возможно - цеолита Y в водородной форме, сушку и прокаливание катализатора, отличающийся ...

VERFAHREN ZUM REFORMIEREN VON KOHLENWASSERSTOFFHALTIGEN EINSATZSTOFFEN ÜBER EINEN FÜR SCHWEFEL EMPFINDLICHEN KATALYSATOR

VORSCHWEFELUNGSZUSAMMENSETZUNG FUER WASSERSTOFFBEHANDLUNGSKATALYSATOREN.

Verfahren zur Herstellung von Katalysatoren.

VERFAHREN ZUR OKTANZAHLSTEIGERUNG UND ZUR VERRINGERUNG DES SCHWEFELGEHALTES VON OLEFINISCHEN BENZINEN.

HYDROTREATMENT PROCESS

PREPARATION OF MODIFIED ZEOLITES

Catalytically upgrading sulphur rich naphtha

DEVICE TO FACILITATE PUTTING AN ELASTIC ENVELOPE ON A PART PROJECTING FROM THE HUMAN BODY AND A METHOD OF EXPANDING THE CROSS SECTION OF THE ENVELOPE

PREPARATION OF MODIFIED ZEOLITES

Catalytic treatment of gas oils

The invention relates to the catalytic treatment of a gas oil feed stock, distilling between 150 DEG and 530 DEG C., in a reactor zone whose temperature is comprised between 200 DEG and 500 DEG C., the pressure is comprised between 15 and 80 bars and containing a hydrogen form zeolite as catalyst, in the presence of a quantity of isobutane representing from 5 to 100% of said feed stock. The process is particularly suitable for the improvement of the filtration temperature limit of the gas oils.

Molecular sieve catalyst suitable for hydrocarbon conversion processes

A hydrocarbon conversion catalyst of uniform pore size 6-15 is prepared by heating a mixture of solutions of sodium silicate and aluminate to obtain precipitated sodium aluminosilicate, base-exchanging with an ammonium compound and calcining the product to obtain the hydrogen form of the crystal which is then impregnated with a metal compound of the platinum group or with an oxide of Mo, Cr, W, V, Ni, Cu or Co or a mixture thereof; the proportions of the starting materials are such that the silica/alumina ratio in the final molecular sieve support is in the range 2,2-10:1 and the Na content is not more than 10% (calculated as Na2O). Specification 824,543 is referred to.

CATALYTIC SYSTEM AND PROCESS FOR THE TOTAL HYDROCONVERSION OF HEAVY OILS

Catalytic system and process for the total hydroconversion of heavy oils

Catalytic system and process for the total hydroconversion of heavy oils

Catalytic system and process for the total hydroconversion of heavy oils

ZEOLITES

HYDROENTMETALLISIERUNG AND HYDRAULIC DESULPHURISATION WITH A CATALYST WITH SPECIFIED MACRO POROSITY.

Countercurrent desulfurization process for refractory organosulfur heterocycles

Process for extruding cystalline aluminosilicates

ZEOLITES

HYDROGENATION PROCESS

CATALYTIC SYSTEM FOR HYDROCONVERSION OF NAPHTHA

A hydroconversion catalyst for hydrodesulfurizing feedstock while preserving octane number of the feedstock includes a support having a mixture of zeolite and alumina, the zeolite having an Si/Al ratio of between about 1 and about 20, and an active phase on the support and including a first metal selected from group 6 of the periodic table of elements, a second metal selected from the group consisting of group 8, group 9 and group 10 of the period table of elements and a third element selected from group 15 of the periodic table of elements. A hydroconversion process is also disclosed.

HYDROTREATING CATALYST AND PROCESS

CRYSTALLINE SILICATES PROCESS FOR THEIR PREPARATION AND CATALYTIC CONVERSIONS USING THEM

Crystalline silicates having: a) a certain specific X-ray powder diffraction pattern; b) a composition expressed in moles of the oxides: p(0.9 ? 0.3)M2/nO . p(a X2O3 . b Y2O3) . SiO2, wherein M = H and alkali metal and/or alkaline earth metal, X = rhodium, chromium and/or scandium, Y = aluminium, iron and/or gallium, a > 0.5, b > 0, a + b = 1, 0 < p < 0.1 and n = the valency of M. Process for the preparation of these silicates and process for carrying out chemical conversions using catalysts comprising the silicates.

HYDROCARBON CONVERSION CATALYST

HYDROCARBON CONVERSION CATALYST Hydrocarbon conversion catalyst comprising an active metallic component comprising at least one metal having hydrocarbon conversion activity and at least one oxygenated phosphorus component, and a support component comprising at least one porous refractory inorganic oxide matrix component and at least one crystalline molecular sieve zeolite component.

CATALYTIC TREATMENT OF GASOILS

Procédé de traitement pour l'amélioration des propriétés d'écoulement d'une coupe gas oil. Le procédé est caractérisé en ce qu'on traite la charge de gas oil d'intervalle de distillation 150-530.degree.C dans une zone réactionnelle dont la température est comprise entre 200 et 500.degree.C, la pression est comprise entre 15 et 80 bars et qui contient une zéolithe sous forme protonée comme catalyseur, en présence d'une quantité d'isobutane représentant de 5 à 100% de ladite charge. Le procédé est notamment utilisable pour l'amélioration de la température limite de filtrabilité des gas oils.

HYDROTREATING CATALYST AND PROCESS

HYDRODESULFURIZATION OF PETROLEUM RESIDUA

MULTI-STAGE HYDRODESULFURIZATION OF CRACKED NAPHTHA STREAMS WITH INTERSTAGE FRACTIONATION

A process for the selective hydrodesulfurization of olefinic naphtha streams containing a substantial amount of organically bound sulfur and olefins. The olefinic naphtha stream is selectively hydrodesulfurized in a first sulfur removal stage and resulting product stream, which contains hydrogen sulfide and organosulfur is fractionated at a temperature to produce a light fraction containing less than about 100 wppm organically bound sulfur and a heavy fraction containing greater than about 100 wppm organically bound sulfur. The light fraction is stripped of at least a portion of its hydrogen sulfide and can be collected or passed to gasoline blending. The heavy fraction is passed to a second sulfur removal stage wherein at least a portion of any remaining organically bound sulfur is removed.

METHOD FOR PREPARING HYDROGENATION PURIFICATION CATALYST

A method for preparing a hydrogenation purification (de-metallization) catalyst containing an inorganic oxide carrier and a metal active for hydrogenation and exhibiting a bimodal pore characteristic wherein pores of a pore diameter of 50 nm or less have a pore volume of 0.4 cm3/g and pores of a pore diameter of 50 nm or more have a pore volume of 0.2 cm3/g or more, and pores of a pore diameter of 1000 nm or more have a pore volume of 0.1 cm3/g or less, which comprises a step of subjecting a quasi-boehmite powder having a peptization index of 0.13 to 0.28 to mixing and forming, and a step of firing the formed quasi-boehmite under a condition wherein the quasi-boehmite is converted to .gamma.-alumina. The method allows the preparation of a hydrogenation purification catalyst exhibiting a bimodal pore characteristic with ease and simplicity at a reduced cost.

PROCESS FOR THE PRODUCTION OF MEDICINAL WHITE OIL USING M41S AND SULFUR SORBENT

A four stage process for producing high quality white oils, particularly food or medicinal grade mineral oils from mineral oil distillates. The first reaction stage employs a sulfur resistant hydrotreating catalyst and produces a product suitable for use as a high quality lubricating oil base stock. The second reaction stage employs a hydrogenation/hydrodesulfurization catalyst. The third stage employs a reduced metal sulfur sorbent producing a product stream which is low in aromatics and which has substantially "nil sulfur". The final reaction stage employs a selective hydrogenation catalyst that produces a product suitable as a food or medicinal grade white oil.

HYDROCARBON FEED HYDRO CRAKING OR CRACKING CATALYST

BASE METAL DEWAXING CATALYST

Methods are provided for making base metal catalysts with improved activity. After forming catalyst particles based on a support comprising a zeolitic molecular sieve, the catalyst particles can be impregnated with a solution comprising a) metal salts (or other precursors) for a plurality of base metals and b) an organic dispersion agent comprising 2 to 10 carbons. The impregnated support particles can be dried to form a base metal catalyst, and then optionally sulfided to form a sulfided base metal catalyst. The resulting (sulfided) base metal catalyst can have improved activity for cloud point reduction and/or for improved activity for heteroatom removal, relative to a base metal dewaxing catalyst prepared without the use of a dispersion agent.

TRIM DEWAXING OF DISTILLATE FUEL

Methods and catalysts are provided for performing dewaxing of diesel boiling range fractions, such as trim dewaxing, that allow for production of diesel boiling range fuels with improved cold flow properties at desirable yields. In some aspects, the methods can include use of dewaxing catalysts based on an MEL framework structure (ZSM-11) to provide improved dewaxing activity. In some aspects improved dewaxing is achieved operating at lower pressures and with higher amounts of organic nitrogen slip from hydrotreatment.

PROCESS TO MANUFACTURE LUGE OIL PRODUCTS

The instant invention relates to a process to produce lube oil products through the hydrotreating of lube ail boiling range feedstreams in the presence of a bulk metal hydrotreating catalyst comprising: i) a Group VIB metal component selected from molybdenum, tungsten and mixtures thereof; ii) a Group V metal component selected from vanadium, niobium, tantalum and mixtures thereof; and iii) a Group VIII metal component selected from nickel, cobalt, iron, and mixtures thereof, wherein the metal components (calculated as oxides) comprise at least 50 wt. % of the catalyst, wherein the molar ratio between the metal components satisfies the formula (Group VIB + Group V) : (Group VIII)=0.35-2,1.

HYDROCARBON CONVERSION CATALYSTS

PROCESS FOR PRODUCING A HYDROCARBON COMPONENT

BORIUM-CONTAINING CATALYST

A catalyst composition for converting hydrocarbons in a hydrotreatment process (hydrodesulfurization and/or hydrodenitrogenization) and simultaneously cracking them, containing an alumina-silica-alumina carrier built up from alumina and silica-alumina, on which hydrogenation metals, such as molybdenum, nickel, and/or cobalt, have been provided and which also contains a catalytically active amount of boron, generally in the range of 1 to 20 wt.%. The invention also relates to a process for the preparation of such a catalyst, with boron being provided ahead of the Group VIII component. The carrier material used may be made up of mixtures of alumina and amorphous silica-alumina or of mixtures of alumina and silica- coated alumina. The catalyst composition is highly suitable for converting vacuum gas oil into middle distillate oils by hydrotreating.

HYDROGENATION PROCESS

... 2112261 9302157 PCTABS00019 A hydrogenation process for reducing the unsaturation of lubricants uses a catalyst which is based on an ultra-large pore crystalline material. The crystalline material has pores of at least 1.3 nm (13 Å) diameter arranged in a uniform manner and exhibits unusually large sorption capacity demonstrated by its benzene adsorption capacity of greater than 15 grams benzene/100 grams (6.7 kPa/50 torr and 25 ·C). A preferred form of the catalyst has a hexagonal structure which exhibits a hexagonal electron diffraction pattern that can be indexed with a d100 value greater than 1.8 nm (18 Å). The hydrogenation catalysts based on these materials are capable of reducing the unsaturation in poly alpha olefin lubricants to a low level.

ZEOLITE NU-85

A zeolite, designated NU-85, is an intergrowth of zeolites EU-1 and NU-87. The zeolite is a useful catalyst in a wide variety of hydrocarbon conversion reactions including isomerisation and alkylation.

PROCESS FOR THE DEMETALLATION OF RESIDUAL OILS

Process for the demetallation of petroleum crude oil by contacting the oil together with hydrogen with a catalyst having at least one metal or compound thereof of Group VIII and/or Group VI of the Periodic Table as its active material supported on a carrier comprising a zeolite with a SiO2/Al2O3 ratio of at least 5 and a unit cell size of between 24.30 and 24.60.

HYDROCARBON UPGRADING PROCESS

F-6456 HYDROCARBON UPGRADING PROCESS In a process for upgrading a sulfur containing feed fraction boiling in the gasoline boiling range, the feed is contacted with a hydrotreating catalyst, which comprises a) a zeolite having a Constraint Index of 1 to 12, preferably MCM-22, b) a Group VI metal, c) a Group VIII metal, and d) a refractory support, under hydrotreating conditions such as to produce a product comprising a normally liquid fraction which boils in substantially the same boiling range as the feed fraction, but which has a lower sulfur content than, and a research octane number (RON) substantially no less than, the feed fraction.

SELECTIVE HYDRODESULFURIZATION CATALYST AND PROCESS

A catalyst and process for hydrodesulfurizing naphtha feedstreams wherein th e reactor inlet temperature is below the dew point of the feedstock at the reactor inlet so that the naphtha will completely vaporize within the catalyst bed. The catalyst is comprised of about 1 to about 10 wt.% MoO3, about 0.1 to about 5 wt.% CoO supported on a suitable support material. They are also characterized as having an average medium pore diameter from about 60 .ANG. to 200 .ANG., a Co/Mo atomi c ratio of about 0.1 to about 1.0, a MoO3 surface concentration of about 0.5 .times. 10 -4 to about 3.0 .times. 10 -4 g MoO3/m2, and an average particle size of less than about 2.0 mm in diameter.

Verfahren zur Herstellung eines Katalysators, Katalysator und dessen Verwendung

DEVICE FOR THE RELIEF OF TIGHTENING A FLEXIBLE COVERING TO A OF A HUMAN KOERPER MANAGING PART.

Antibiotic A/16686 and its preparation from actinoplanes

СПОСОБ ПЕРЕРАБОТКИ УГЛЕВОДОРОДНОГО СЫРЬЯ (ВАРИАНТЫ)

Изобретение относится к области нефтехимии - к способам переработки углеводородного сырья, имеющего температуру конца кипения от 140 до 400°С, и предназначено для получения топливных фракций - бензиновых, керосиновых и/или дизельных фракций при помощи твердых катализаторов. В качестве сырья возможно использование фракций нефти, газового конденсата или его фракций, продуктов переработки нефтяных, газоконденсатных фракций и других углеводородных фракций, например, продуктов процесса Фишера-Тропша и т.п. Переработку сырья в целом осуществляют путем его контактирования с регенерируемым катализатором при температуре 250-500°С и скорости подачи сырья до 10 ч-1 и последующего разделения продуктов реакции путем сепарации и/или ректификации на газообразную(ые) фракцию(и), бензиновую, керосиновую и/или дизельную фракции. По одному варианту превращение сырья осуществляют при давлении 0,1-4,0 МПа на катализаторе, содержащем цеолит или силикат со структурой ZSM-5 или ZSM-11 общей эмпирической формулы ...

СПОСОБ ПЕРЕРАБОТКИ УГЛЕВОДОРОДНОГО СЫРЬЯ

Изобретение относится к области нефтепереработки и нефтехимии - к способам переработки углеводородного сырья, имеющего температуру конца кипения от 140 до 400°С, и предназначено для получения топливных фракций - бензиновых, керосиновых и/или дизельных фракций при помощи твердых катализаторов. В качестве сырья возможно использование нефтяных фракций, газового конденсата или его фракций, вторичных продуктов переработки нефти и газового конденсата и других углеводородных фракций, например продуктов процесса Фишера-Тропша и т.п. Переработку сырья в целом осуществляют путем его контактирования с регенерируемым катализатором при температуре 250-500°С, давлении 0, 1-6,0 МПа и скорости подачи сырья до 10 ч-1 и последующего разделения продуктов реакции путем сепарации и/или ректификации на газообразную(ые) фракцию(и), бензиновую, керосиновую и/или дизельную фракции. В процессе используют катализаторы, содержащие цеолиты со структурой ZSM-5 или ZSM-11, в т.ч. модифицированные элементами I-VIII групп ...

Coal tar hydrogenation catalyst, and preparation method and application thereof

Hydrogenation catalyst, preparation method thereof, and coal-tar hydrogenation process

A Beta/ZSM - 12 symbiotic zeolite molecular sieve and its preparation method

Method for preparing mercaptan conversion catalyst in petroleum

The present invention discloses a method for preparing a mercaptan conversion catalyst in petroleum, comprising: activating a carrier; preparing a soaking solution containing a cobalt phthalocyanine compound and a soaking solvent; soaking the activated carrier in the soaking solution to perform an ultrasonic treatment to obtain mixed materials; filtering a load carrier from the mixed materials, and drying in an vacuum to obtain a catalyst precursor; soaking the precursor in an inorganic alkali solution to perform a second ultrasonic treatment; and filtering a secondary carrier from the mixture experiencing the second ultrasonic treatment, and drying in an vacuum to obtain the mercaptan conversion catalyst in the petroleum. In the preparation method according to the present invention, the mixed materials obtained upon being soaked are subjected to an ultrasonic treatment. This improves the solubility of the molecules of the cobalt phthalocyanine compound in the soaking solution, quickens ...

Catalyst of deep additional treatment of hydrogenising base oil for lubricant, preparation method and application

The invention relates to a catalyst which is used in hydrogenation deepness supply prepared by the lubricating oil base oil and its preparation method and application, the catalyst takes one or serveral kind of the porous materialgamma-aluminum oxide, the compound nanometer zirconium oxide/gamma-aluminum oxide, the compound nanometer titamium oxide/gamma-aluminum oxide, the compound nanometer silica/gamma-aluminum oxide, new type hole MCM-41 molecular sieve or the MCM-41 molecular sieve of the aluminum modified as the carrier, the catalyst which is composed by nickel molybdenum bimetal nitride whose chemical formula is the Ni2Mo3N and the weight of the load is 7% to 50%, confects the dipping fluid by nickelous nitrate and ammonium molybdate, of which the Ni density is 0.2 to 2.0mol/L, the Mo density is 0.3 to 3.5mol/L, the mole ratio of Ni and Mo is 0.55 to 0.75:1; takes the dipping fluid according to the 2-10 time volumes of carrier soakage to soak the carrier; prepares the dipping carrier ...

Hydrofining method of low-grade gasoline/diesel oil

Lubricating oil base oil hydrofining technology

BASED CATALYST AND/2 A-ACETYLBUTYROLACTONE OR ITS HYDROLYSIS PRODUCTS AND ITS USE IN A METHOD OF HYDROTREATING OR HYDROCRACKING/AND

CATALYST CONTAINING METALS OF GROUP VI AND GROUP VIII PRESENT AT LEAST ENPARTIE IN the FORM Of HETEROPOLYANIONS IN the PRECURSOR OXIDIZES

CATALYST IS STABLE IN A HIGH RETENTION CAPACITY AND METALS, USES FOR THE DEMETALLIZATION OF HEAVY CRUDES, AND METHOD OF MAKING SAME

CATALYSTS Of HYDROCARBON HYDRO-TREATING AND APPLICATIONS OF THESE CATALYSTS

Zéolithe de type mordenite et son procédé de préparation.

L'invention a pour objet une zéolithe cristalline synthétique de type mordénite caractérisée en ce qu'elle possède: a) la formule générale approchée suivante (CF DESSIN DANS BOPI) où x est un nombre compris entre 9 et 30, et b) un diagramme de diffraction des rayons X représenté dans le tableau I de la description, et en ce qu'elle a été synthétisée en milieu fluorure. L'invention concerne également un procédé de préparation de ladite zéolithe. Cette zéolithe peut être utilisée notamment en adsorption et en catalyse.

METHOD FOR THE MANUFACTURE OF AN EXTRUDED CATALYST AND THE USE THEREOF

Hydrorefining of petroleum charges involves using catalyst comprising partially amorphous zeolite Y, matrix and a hydro-dehydrogenating element

The catalysts shows a high activity in reactions of hydrogenation of aromatics, hydrodeazotisation and hydrodesulfuration, due to the presence of the amorphous zeolite, the effect being enhanced by the inclusion of boron and silicon in the matrix. A hydrorefining process for hydrocarbon charges uses a catalyst comprising a matrix, a hydro-dehydrogenating element, a zeolite Y, partially amorphous with a peak intensity (X-ray diffraction pattern) less than 0.4 and a crystalline fraction (relative to a zeolite of Na form) less than 60%.

HYDROTREATING CATALYST AND PROCESS

catalisador zeolìtico com teor controlado em elemento dopador e processo melhorado de tratamento de cargas hidrocarbonadas

COMPOSED OF ZEOLITE METHOD TO OBTAIN IT AND CATALYTIC APPLICATION OF THE SAME

Un material catalítico que incluye zeolita microporosa sobre un soporte de oxido inorgánico mesoporoso. La zeolita microporosa puede incluir zeolita b, zeolita Y (incluyendo ôultra estable Yö - USY), modernita, Zeolita L, ZSM-5, ZSM-11, ZSM-12, ZSM-20, q-1, ZSM-23, ZSM-34, ZSM-35, ZSM-48, SSZ-32, PSH-3, MCM-22, MCM-49, MCM-56, ITQ-1, ITQ-2, ITQ-4, ITQ-21, SAPO-5, SAPO-11, SAPO-37, breck-6, ALPO4-5, etc.. El oxido inorgánico mesoporoso puede ser, por ejemplo, silica o silicato. El material catalítico puede ser además modificado introduciendo algunos metales, por ejemplo, aluminio, titanio, molibdeno, níquel, cobalto, hierro, tungsteno, paladio, y platino. Puede ser utilizado para reacciones de acilacion, alquilacion, dimerizacion, oligomerizacion, polimerizacion, hidrogenacion, dehidrogenacion, aromatizacion, isomerizacion, hidrotratamiento, cracking catalítico e hidrocracking. Reivindicacion 1: Una composicion que comprende: a) al menos un tipo de un material cristalino y microporoso con ...

HYDROGENATION DESULFURIZATION CATALYST FOR DIESEL OIL AND HYDROGENATION TREATMENT METHOD FOR DIESEL OIL

This catalyst is a hydrogenation desulfurization catalyst that supports one or more metals selected from a group formed from the group 6 elements of the long period periodic table, one or more metals selected from a group formed from the group 9 elements and the group 10 elements of the same, phosphorus, and an organic acid on a composite oxide carrier having a specific content of both alumina and HY zeolite having a specific crystallite size and the like. The catalyst basis in an oxide conversion includes 10 - 40% by mass of the group 6 metal, 1 - 15% by mass of the group 9 and group 10 metals, and 1.5 - 8% by mass phosphorus. The catalyst basis in an element conversion includes 0.8 - 7 percent by mass of carbon derived from an organic acid and for each mole of the group 9 element and group 10 element metals, the same includes 0.2 - 1.2 moles of the organic acid. The average poor diameter at a specific surface area, pore volume, and pore distribution is within a specific range.

BASE METAL DEWAXING CATALYST

Methods are provided for making base metal catalysts with improved activity. After forming catalyst particles based on a support comprising a zeolitic molecular sieve, the catalyst particles can be impregnated with a solution comprising a) metal salts (or other precursors) for a plurality of base metals and b) an organic dispersion agent comprising 2 to 10 carbons. The impregnated support particles can be dried to form a base metal catalyst, and then optionally sulfided to form a sulfided base metal catalyst. The resulting (sulfided) base metal catalyst can have improved activity for cloud point reduction and/or for improved activity for heteroatom removal, relative to a base metal dewaxing catalyst prepared without the use of a dispersion agent.

NAPHTHA PRODUCTION FROM REFINERY FUEL GAS

Systems and methods are provided for upgrading refinery fuel gas and/or production of naphtha from refinery fuel gas. Initially, an olefin-containing feed can be exposed to conventional conditions for removing a portion of C3+ compounds and a portion of sulfur-containing compounds. The olefin-containing feed can then be exposed to conversion conditions for the oligomerization of olefins present in the olefin-containing feed, producing an effluent that includes C5+ olefins. The C5+ olefins can be removed from the effluent, and the effluent can then be subjected to an amine wash to remove sulfur- containing compounds. The resulting product effluent includes a refinery fuel gas product having a controlled energy content.

CATALYST STRUCTURE FOR CATALYTIC CRACKING OR HYDRODESULFURIZATION, CATALYTIC CRACKING DEVICE AND HYDRODESULFURIZATION DEVICE USING SAID CATALYST STRUCTURE, AND PRODUCTION METHOD FOR CATALYST STRUCTURE FOR CATALYTIC CRACKING OR HYDRODESULFURIZATION

Provided is a catalyst structure for catalytic cracking or hydrodesulfurization which is capable of suppressing a reduction in catalyst activity to enable an efficient catalytic cracking treatment and makes it possible to easily and stably obtain a reformed product. This catalyst structure (1) for catalytic cracking or hydrodesulfurization comprises a carrier (10) with a porous structure composed of a zeolite compound, and metal oxide microparticles (20) of at least one type of metal oxide in the carrier (10), wherein the carrier (10) has interconnecting passages (11), the metal oxide microparticles (20) are present in at least the passages (11) in the carrier (10), and the metal oxide microparticles (20) are composed of a material containing one or more of oxides of Fe, Al, Zn, Zr, Cu, Co, Ni, Ce, Nb, Ti, Mo, V, Cr, Pd and Ru.

COUNTERCURRENT DESULFURIZATION PROCESS FOR REFRACTORY ORGANOSULFUR HETEROCYCLES

L'invention concerne un processus d'hydrodésulfuration (HDS) de multiples composés organo-sulfureux à noyau hétérocycliques condensés, présents dans le pétrole et les courants chimiques. Le courant passe par au moins une zone de réaction à contre-courant par rapport à un flux gazeux de traitement contenant de l'hydrogène, et par au moins une zone de sorbant. La zone de réaction contient un lit de catalyseur d'hydrodésulfuration contenant un métal du groupe VIII et la zone de sorbant contient un lit de matière sorbante d'hydrogène sulfuré.

TWO STAGE DIESEL FUEL HYDROTREATING AND STRIPPING IN A SINGLE REACTION VESSEL

A diesel fraction is purified by a process having two reaction stages represented by (14) and (18) and a stripping stage in a single vessel. Heteroatoms are removed in the first stage (14), to permit the use of a sulfur sensitive aromatics saturation catalyst in the second stage, to produce a purified diesel stock. The first stage liquid effluent is stripped in a stripping stage and then passed into the second reaction stage (18), in which it reacts with fresh hydrogen for aromatics removal. The second reaction stage (18) produces a hydrogen-rich vapor effluent, which may provide all or a portion of the first stage (18). The diesel feed for the process may be one that has been at least partially refined with respect to either or both heteroatom or aromatics removal.

Introducing mesoporosity into zeolite materials with a modified acid pre-treatment step

Methods for introducing mesoporosity into zeolite materials that employ an acid pretreatment step are provided. By utilizing a non-acidic chelating agent during the acid treatment step, the zeolite material can be pretreated with a strong acid, often in higher concentrations or over shorter contact times, than had previously been contemplated. The resulting acid-treated mesoporous materials retain desirable properties, including Si/Al, UCS, and total mesopore and micropore volume. The ability to use a stronger acid without damaging the zeolite material results in a less expensive process capable of producing mesoporous zeolite materials suitable for a wide range of uses.

HYDROGENATION WITH A Y TYPE ZEOLITE-ARSENIC CATALYST

Hydrogenation of a mineral oil containing aromatic hydrocarbons by use of a hydrogenation catalyst comprised of a Y-zeolite containing arsenic.

Catalyst for the hydroisomerization of contaminated hydrocarbon feedstock

A catalyst system for treating sulfur and nitrogen contaminated hydrocarbon feedstock includes a matrix, at least one support medium substantially uniformly distributed through said matrix and comprising a silica alumina molecular sieve material having a silica/alumina ratio of at least about 20, a first catalytically active metal phase supported on said support medium, said first catalytically active metal phase comprising a first metal and a second metal each selected from group VIII of the Periodic Table of Elements, said first metal being different from said second metal, a second catalytically active metal phase supported on said matrix, said second catalytically active metal phase comprising a third metal and a fourth metal each selected from group VIII of the Periodic Table of Elements and a fifth metal selected from group VIb of the Periodic Table of Elements, said third metal being different from said fourth metal. The catalyst system has a higher ratio of silica to alumina in ...

Process for the preparation of light fuels

In the process of the invention, an aliphatic C2-C14 hydrocarbon product is prepared from natural fats or derivatives thereof. The process comprises the steps of: (i) providing a natural fat or derivative thereof, (ii) deoxygenating a natural fat or derivative thereof originating from step (i) to yield an aliphatic C9-C28 hydrocarbon, (iii) hydrocracking an aliphatic C9-C28 hydrocarbon originating from step (ii) to yield a product comprising an aliphatic C2-C14 hydrocarbon, (iv) isomerising an aliphatic C2-C14 hydrocarbon originating from step (iii) into an isomerised aliphatic C2-C14 hydrocarbon, and optionally (v) recovering an isomerised C2-C14 hydrocarbon originating from step (iv) as said C2-C14 hydrocarbon product. Pure and high quality light fuel is easily obtained in sufficient amounts.

Steam reforming reactor for synthesis gas production

Steam reforming reactor for the preparation of hydrogen and carbon monoxide rich gas comprising a porous supporting structure adhered to the wall of the reforming reactor, the porous supporting structure being coated with catalyst containing a ceramic precursor, and impregnated with the catalytic active material.

CATALYST COMPRISING A PARTIALLY AMORPHOUS ZEOLITE Y AND ITS USE IN HYDROCONVERSION OF HYDROCARBON OIL FEEDSTOCKS

Crystalline silicoaluminophosphates

Catalyst composition with modified silica-alumina support

Hydrocarbon conversion catalyst comprising noble metal on a rare earth and group IVB oxides modified silica-alumina support

HYDROGENATION TREATMENT CATALYST FOR COAL LIQUEFACTION SOLVENT

PURPOSE: To make a coal liquefaction operation steady for a long time by supporting group VI and VII metals on a catalyst support made of specified amount of γ-alumina and a pentasil-type zeolite of a specified SiO2/Al2O3 ratio. CONSTITUTION: A catalyst support, composed of 80W20wt.% alumina and 20W80wt.% pentasil-type zeolite of 25W100 SiO2/Al2O3 mole ratio, is prepared. A hydrogenation treatment catalyst for coal liquefaction solvent is obtained by having this catalyst support support 5W20wt.% at least one species from group VI metal and 1W10wt.% at least one species from group VII metal in reduced weights of their respective oxides, and by regulating a pore radius distribution measured by mercury porosimetry so that the mean pore radius is 120Å or larger and the accumulated pore volume occupied by the pores with 100Å or larger radii is 60% or larger of that occupied by the pores with 40Å or larger radii. COPYRIGHT: (C)1989,JPO&Japio ...

PRODUCTION OF HYDROTREATED OIL

PROBLEM TO BE SOLVED: To provide a process for producing a hydrotreated oil in good productivity without encountering the problem of the formation of hot spots in the catalyst layer and the solidification of the catalyst layer in the hydrotreatment of heavy hydrocarbon oil. SOLUTION: In a process for producing a hydrotreated oil by bringing a heavy hydrocarbon oil and a hydrogen gas into contact with the catalyst in a catalyst layer, a mixture prepared by combining a metal-supported inorganic oxide catalyst (A) carrying at least one metal selected among the metals of groups 6, 8, 9 and 10 with a zeolite catalyst (B) prepared by bringing a mineral acid solution having a pH of 1.5 or below or a metal salt aqueous solution of at least one member selected among the metals of groups 8, 9 and 10 downstream of the catalyst layer is used. COPYRIGHT: (C)1998,JPO ...

DEMETALLIZATION AND DESULFURIZATION FOR RESIDUAL OIL

HYDROCARBON CONVERTING CATALYST

СПОСОБ КАТАЛИТИЧЕСКОЙ КОНВЕРСИИ ЛЕГКИХ ОЛЕФИНОВ

Изобретение относится к способу получения легких олефинов, включающему ввод исходного сырья - углеводородного масла - в контакт с катализатором каталитической конверсии в реакторе для каталитической конверсии, включающим одну или несколько реакционных зон для проведения реакции, где исходное сырье в виде углеводородного масла подвергают реакции каталитической конверсии в присутствии ингибитора, и отделение пара реагента, произвольно содержащего ингибитор, от кокса, нанесенного на катализатор, а целевое изделие, содержащее этилен и пропилен, получают путем отделения пара реагента, катализатор отделяют от кокса и восстанавливают для повторного использования в реакторе, причем отношения ингибитора к исходному сырью составляет 0,001-15% по весу, ингибитор выбирают из вещества, обладающего способностью вырабатывать водород, или имеющего восстановительную способность, или обладающего адсорбционной способностью на активном центре кислотных катализаторов и их смесей, причем вещество, обладающее ...

КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ ДЛЯ ОБЛАГОРАЖИВАНИЯ УГЛЕВОДОРОДОВ С ТЕМПЕРАТУРАМИ КИПЕНИЯ В ПРЕДЕЛАХ ЛИГРОИНОВОЙ ФРАКЦИИ

FIELD: chemical and petrochemical industries. SUBSTANCE: the invention presents a catalytic composition for enrichment of hydrocarbons with boiling temperatures like naphtha fraction boiling temperatures. the catalytic composition includes zeolite -RS-10, a metal of VIII group, a metal of VI group and possibly one or more oxides in the capacity of the catalyst carrier. According to a preferable version the catalytic composition also includes a metal of IIB and-or III- groups. According to the true invention the catalytic composition may be used for enrichment of hydrocarbonaceous mixes having a range of boiling temperatures within the limits from CC 4 up to 250 o C. It is preferable to use hydrocarbonaceous mixes boiling at the temperatures, that are in the range of boiling temperatures of naphtha fraction, and containing admixtures of sulfur, i.e. for a hydrodesulphuration with a simultaneous sceletal isomerization of olefines contained in these hydrocarbons. At that the whole process is realized in one stage. The invention also offered methods of production of a catalytic composition using impregnation (versions) and a sol-gel technology (versions), a method of desulphuration with use of the stated catalytic composition and zeolite -RS-10. EFFECT: the invention allows to enrich hydrocarbons with boiling temperatures, that are in the range of boiling temperatures of naphtha fraction. 51 cl, 25 ex, 4 tbl 2227066 С2 ко РОССИЙСКАЯ ФЕДЕРАЦИЯ й 7 (19) (11) < ах ; (13) < 2 5 С2 Опубликовано на СО-ВОМ: МПМОЗА ВЕС 200404 — МКЕР2004004 7 # &) 2 ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ИЗВЕЩЕНИЯ К ПАТЕНТУ НА ИЗОБРЕТЕНИЕ ММАА - Досрочное прекращение действия патента СССР или патента Российской Федерации на изобретение из-за неуплаты в установленный срок пошлины за поддержание патента в силе (21) Регистрационный номер заявки: 99127286 Дата прекращения действия патента: 21.12.2009 Извещение опубликовано: 10.11.2010 БИ: 31/2010 Стр.: ...

Способ получения зимних и арктических дизельных топлив из прямогонных дизельных фракций с содержанием серы до 5000 мг/кг и азота до 100 мг/кг

FIELD: oil refining industry. SUBSTANCE: invention relates to the field of oil refining. A method for producing winter and arctic diesel fuels from straight-run diesel fractions with a sulfur content of up to 5000 mg/kg and nitrogen up to 100 mg/kg is described, which provides for sequential processing of raw materials using a catalytic system, characterized by the fact that the raw materials are processed sequentially without intermediate separation of sulfur and nitrogen compounds from the products after the hydrotreating stage, using a catalytic system containing the following layers of catalysts in the direction of movement of raw materials: a preliminary hydrotreating catalyst; a hydrotreating catalyst; a catalyst for the isodeparaffinization of hydrocarbons with increased hydrogenating activity, containing, wt. %: palladium 0.1-0.5, platinum 0.1-0.5, the rest being the carrier, while the carrier contains: EU-2 zeolite 30-80, γ-Al 2 O 3 20-70; an isodeparaffinization catalyst containing, wt. %: platinum 0.4-0.8, the rest carrier, while the carrier contains: EU-2 zeolite 30-80, γ-Al 2 O 3 20-70; a hydrofinishing catalyst. EFFECT: increase in the quality of the target dewaxed products by reducing the content of aromatic hydrocarbons when using straight-run diesel fractions with a sulfur content of up to 5000 mg/kg and nitrogen up to 100 mg/kg. 3 cl, 7 tbl, 5 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 758 846 C1 (51) МПК C10L 1/08 (2006.01) C10G 11/00 (2006.01) C10G 45/64 (2006.01) C10G 45/12 (2006.01) C10G 65/00 (2006.01) B01J 29/74 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10L 1/08 (2021.05); C10G 11/00 (2021.05); C10G 45/64 (2021.05); C10G 45/12 (2021.05); C10G 65/00 (2021.05); B01J 29/74 (2021.05) (21)(22) Заявка: 2021107747, 24.03.2021 24.03.2021 Дата регистрации: 02.11.2021 (45) Опубликовано: 02.11.2021 Бюл. № 31 2 7 5 8 8 4 6 R U (56) Список документов, цитированных в отчете о поиске: WO ...

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА ДЕМЕТАЛЛИЗАЦИИ НЕФТЯНЫХ ФРАКЦИЙ

FIELD: oil and gas industry.SUBSTANCE: invention relates to oil refining industry, in particular, to catalysts for hydro-regeneration of oil fractions. Disclosed is a method of producing a catalyst for demetallisation of petroleum fractions by preliminary preparation of a catalyst support by depositing aluminum hydroxide from a solution of aluminum nitrate or aluminum alkoxide in the presence of an aqueous dispersion of macropore template with particle diameter of 0.1–2.0 mcm in amount of 10–35 wt%. on dry catalyst support, adding zeolite in amount of 5–30 wt% to the obtained mass of the powder. on a dry catalyst support, by molding, drying and calcining, and then applying the active components onto the prepared carrier, by impregnating with a solution of nickel, cobalt and molybdenum precursors. Macropore template is represented by a paraffin emulsion or a dispersion of the styrene-acrylic copolymer. Zeolite used is ultra stable zeolite Y and/or high-silica zeolite ZSM-5. Content of active components in terms of oxides in calcined catalyst is 5.0–7.0 wt%. MoO; 0.5–0.7 wt% CoO; 0.7–1.1 wt% NiO. Produced catalyst has specific surface area of not less than 180 m/g with specific pore volume of not less than 0.25 cm/g.EFFECT: disclosed method of producing a demethallisation catalyst, having adsorption and catalysis functions, provides, in conditions of hydrogenation refining of oil fractions, a removal depth of both nickel and vanadium of 85 % and more.5 cl, 1 tbl, 4 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) (19) RU (51) МПК B01J 32/00 B01J 35/04 B01J 21/04 B01J 37/02 B01J 23/88 C10G 45/08 C10G 45/12 (11) (13) 2 691 069 C1 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 32/00 (2019.02); B01J 35/1019 (2019.02); B01J 35/1042 (2019.02); B01J 35/1066 (2019.02); C10G 45/08 (2019.02); C10G 45/12 (2019.02) (21)(22) Заявка: 2018146842, 27.12.2018 27.12.2018 Дата ...

КАТАЛИЗАТОР ГИДРОИЗОДЕПАРАФИНИЗАЦИИ СРЕДНЕДИСТИЛЛЯТНЫХ УГЛЕВОДОРОДНЫХ ФРАКЦИЙ

Изобретение относится к области нефтепереработки, в частности к разработке катализатора гидроизодепарафинизации среднедистиллятных углеводородных фракций, а именно, смесевого сырья нефтяного и растительного происхождения, с получением базовых компонентов авиационных керосинов и дизельных топлив для арктических условий. Катализатор включает смесь высококремнеземных цеолитов, гидрирующие переходные металлы, промотор и связующее, при этом в качестве смеси высококремнеземных цеолитов содержит бикомпонентную смесь цеолитов: среднепористый цеолит ЦВН структуры пентасил и широкопористый цеолит морденит или цеолит β при массовом соотношении ЦВН : (морденит или цеолит β), соответственно (1-6):1, в качестве гидрирующих переходных металлов содержит оксиды никеля и молибдена, в качестве промотора - смесь оксидов бора и лантана, в качестве связующего - смесь аморфного алюмосиликата и γ-оксида алюминия при следующем соотношении компонентов, % масс.: смесь высококремнеземных цеолитов - 40,0-55,0, гидрирующие ...

Production of Low Color Middle Distillate Fuels

In a process for producing a low color diesel and/or kerosene fuel, a middle distillate feed can be supplied to a reactor having at least one first catalyst bed containing a first desulfurization and/or isomerization catalyst and at least one second catalyst bed containing a decolorization catalyst downstream from the first catalyst bed(s). The feed can be reacted with the hydrogen in the presence of the first catalyst at a temperature from about 290° C. to about 430° C. to produce a first liquid effluent, which can be cooled by about 10° C. to about 40° C. with a quench medium and cascaded to the at least one second catalyst bed. The cooled first liquid effluent can then be reacted with hydrogen in the presence of the decolorization catalyst at a temperature from about 280° C. to about 415° C. to produce a second effluent having an ASTM color less than 2.5.

PROCESS FOR THE PREPARATION OF A CATALYST WHICH CAN BE USED IN HYDROTREATMENT AND HYDROCONVERSION

A process for the preparation of a catalyst from a catalytic precursor comprising a support based on alumina and/or silica-alumina and/or zeolite and comprising at least one element of group VIB and optionally at least one element of group VIII, by impregnation of said precursor with a solution of a C1-C4 dialkyl succinate. An impregnation step for impregnation of said precursor which is dried, calcined or regenerated, with at least one solution containing at least one carboxylic acid other than acetic acid, then maturing and drying at a temperature less than or equal to 200° C., optionally a heat treatment at a temperature lower than 350° C., followed by an impregnation step with a solution containing at least one C1-C4 dialkyl succinate followed by maturing and drying at a temperature less than 200° C. without subsequent calcination step. The catalyst is used in hydrotreatment and/or hydroconversion. 2. A process according to characterised in that the catalytic precursor is a catalyst which has been regenerated.3. A process according to characterised in that that the catalytic precursor contains all of the elements of groups GVIB and if they are present all of the elements of group V111.4. A process according to characterised in that the dialkyl succinate is dimethyl succinate.5. A process according to characterised in that the carboxylic acid is citric acid.6. A process according to characterised in that steps 1) and/or 2) are performed in the presence of water and/or ethanol.7. A process according to characterised in that the maturing steps are performed at a temperature between 17 and 60° C.8. A process according to characterised in that the drying operation in step 1) is performed at a temperature between 100 and 180° C.9. A process according to characterised in that the drying operation in step 2) is performed at a temperature between 50 and 160° C.10. A process according to characterised in that the solution of step 1) and/or step 2) contains at least one ...

METHOD OF PRODUCING REGENERATED HYDROTREATING CATALYST AND METHOD OF PRODUCING PETROLEUM PRODUCTS

A method of producing a regenerated hydrotreating catalyst, including a first step of preparing a hydrotreating catalyst that has been used for hydrotreatment of a petroleum fraction and has a metal element selected from Group 6 elements of the periodic table; a second step of performing regeneration treatment for part of the catalyst prepared in the first step, then performing X-ray absorption fine structure analysis for the catalyst after the regeneration treatment, and obtaining regeneration treatment conditions in which a ratio IS/IO of a peak intensity IS of a peak attributed to a bond between the metal element and a sulfur atom to a peak intensity IO of a peak attributed to a bond between the metal element and an oxygen atom is in the range of 0.1 to 0.3 in a radial distribution curve obtained from an extended X-ray absorption fine structure spectrum. 1. A method of producing a regenerated hydrotreating catalyst , comprising:a first step of preparing a hydrotreating catalyst that has been used for hydrotreatment of a petroleum fraction and has a metal element selected from Group 6 elements of the periodic table;{'sub': S', 'O', 'S', 'O, 'a second step of performing regeneration treatment for part of the catalyst prepared in the first step, then performing X-ray absorption fine structure analysis for the catalyst after the regeneration treatment, and obtaining regeneration treatment conditions in which a ratio I/Iof a peak intensity Iof a peak attributed to a bond between the metal element and a sulfur atom to a peak intensity Iof a peak attributed to a bond between the metal element and an oxygen atom is in the range of 0.1 to 0.3 in a radial distribution curve obtained from an extended X-ray absorption fine structure spectrum; and'}a third step of performing regeneration treatment under regeneration treatment conditions determined based on the second step, for the other part of the catalyst prepared in the first step.2. The method of producing a regenerated ...

A CATALYST AND PROCESS FOR THE MANUFACTURE OF ULTRA-LOW SULFUR DISTILLATE PRODUCT

Described is a catalyst and process useful in the hydrodesulfurization of a distillate feedstock to manufacture a low-sulfur distillate product. The catalyst comprises a calcined mixture of inorganic oxide material, a high concentration of a molybdenum component, and a high concentration of a Group VIII metal component. The mixture that is calcined to form the calcined mixture comprises molybdenum trioxide in the form of finely divided particles, a Group VIII metal compound, and an inorganic oxide material. The catalyst is made by mixing the aforementioned starting materials and forming therefrom an agglomerate that is calcined to yield the calcined mixture that may be used as the catalyst or catalyst precursor. 1. A composition for use as a distillate hydrodesulfurization catalyst in the manufacture of an ultra-low sulfur distillate product , wherein said composition comprises:a calcined mixture made by calcining a co-mulled mixture comprising an inorganic oxide material, molybdenum trioxide in the form of finely divided particles having a maximum dimension of less than 150 μm, and a Group VIII metal compound selected from the group consisting of a nickel compound, a cobalt compound and a combination thereof, wherein said calcined mixture has a molybdenum content in the range of from 10 weight percent to 22 weight percent with the weight percent being based upon the molybdenum as metal and the total weight of said calcined mixture, and a Group VIII metal content in the range of from 3 weight percent to 12 weight percent with the weight percent being based upon the Group VIII metal in its elemental form and the total weight of said calcined mixture, wherein said calcined mixture has a mean pore diameter in the range of from 50 angstroms to 100 angstroms, and wherein said calcined mixture has less than 1 percent of the total pore volume in macropores having a diameter greater than 1000 angstroms.2. A composition as recited in claim 1 , wherein said pore structure is ...

PROCESS FOR COMBINED HYDRODESULFURIZATION AND HYDROCRACKING OF HEAVY HYDROCARBONS

The present invention relates to a process for combined hydrodesulfurization and hydrocracking of a heavy hydrocarbon feed comprising contacting the hydrocarbon feed in the presence of hydrogen with a catalyst comprising a mixture of a solid acid catalyst and a hydrodesulfurization catalyst. 1. A process for combined hydrodesulfurization and hydrocracking of a heavy hydrocarbon feed comprising:contacting said heavy hydrocarbon feed in the presence of hydrogen at process conditions comprising a temperature of 350-475° C. and a pressure of 2500-4500 kPa, with a catalyst comprising a mixture of a solid acid catalyst and a hydrodesulfurization catalyst,wherein said hydrodesulfurization catalyst comprises 1-30 wt-% of an element selected from Group 6 of the Periodic Table of Elements based on the total weight of the hydrodesulfurization catalyst, and 0.1-10 wt-% of an element selected from Groups 9 and 10 of the Periodic Table of Elements based on the total weight of the hydrodesulfurization catalyst and a solid catalyst support, and{'sub': 2', '2', '3, 'wherein said solid acid catalyst is comprises an aluminosilicate zeolite having a SiO/AlOmolar ratio of 50-120.'}2. The process according to claim 1 , wherein the element selected from Groups 9 and 10 of the Periodic Table of Elements is Co and/or Ni.3. The process according to claim 1 , wherein the element in the hydrodesulfurization catalyst is in sulfide form.4. The process according to claim 1 , wherein the hydrodesulfurization catalyst comprises one or more selected from the group consisting of CoMoS claim 1 , NiMoS claim 1 , NiWSand CoWS.5. The process according to claim 1 , wherein the solid acid catalyst comprises aluminosilicate zeolite having a 12-ring structure.6. The process according to claim 5 , wherein the aluminosilicate zeolite has super cages having a size of 12-14 Å.7. The process according to claim 5 , wherein the aluminosilicate zeolite is zeolite Y.8. The process according to claim 5 , wherein the ...

HYDROCARBON OIL DESULFURIZATION ADSORBING AGENT, PRODUCTION AND USE THEREOF

This disclosures provides an adsorbent which, on the basis of the total weight of the adsorbent, comprises: 1) a Si—Al molecular sieve having an A-FAU structure, wherein A represents a monovalent cation, in an amount of 1-20 wt %, 2) at least one binder selected from the group consisting of titanium dioxide, stannic oxide, zirconium oxide and alumina, in an amount of 3-35 wt %, 3) a silica source, in an amount of 5-40 wt %, 4) zinc oxide, in an amount of 10-80 wt %, and 5) at least one promoter metal selected from the group consisting of cobalt, nickel, iron and manganese, based on the metal, in an amount of 5-30 wt %, wherein at least 10 wt % of the promoter metal is present in a reduced valence state. This adsorbent exhibits improved activity and stability, and at the same time, is capable of significantly improving the octane number of the product gasoline. 1. A desulfurization adsorbent for hydrocarbon oil , on the basis of the total weight of the adsorbent , comprising the following components ,1) a Si—Al molecular sieve having an A-FAU structure, wherein A represents a monovalent cation, in an amount of 1-20 wt %,2) at least one binder selected from the group consisting of titanium dioxide, stannic oxide, zirconium oxide and alumina, in an amount of 3-35 wt %,3) a silica source, in an amount of 5-40 wt %,4) zinc oxide, in an amount of 10-80 wt %, and5) at least one promoter metal selected from the group consisting of cobalt, nickel, iron and manganese, based on the metal, in an amount of 5-30 wt %, wherein at least 10 wt % of the promoter metal is present in a reduced valence state.2. The adsorbent according to claim 1 , wherein the Si—Al molecular sieve having an A-FAU structure is in an amount of 2-15 wt % claim 1 , the binder is in an amount of 5-25 wt % claim 1 , the silica source is in an amount of 10-30 wt % claim 1 , the zinc oxide is in an amount of 25-70 wt % claim 1 , the promoter metal is in an amount of 8-25 wt %.3. The adsorbent according to claim ...

CATALYST CONTAINING METAL CLUSTER IN STRUCTURALLY COLLAPSED ZEOLITE, AND USE THEREOF

This invention relates to a hydrogen spillover-based catalyst and use thereof, wherein a hydrogen activation metal cluster is dispersed in the form of being encapsulated in a crystalline or amorphous aluminosilicate matrix which is partially or fully structurally collapsed zeolite, thereby exhibiting high hydroprocessing or dehydrogenation activity and suppressed C—C hydrogenolysis activity. 1. A hydrogen spillover-based catalyst , comprising:crystalline or amorphous aluminosilicate formed by partial or full structural collapse of zeolite having a silica/alumina molar ratio of 2 or less; anda hydrogen activation metal (M) cluster encapsulated in the aluminosilicate, {'br': None, 'i': H/M', '+H/M', '+H/M', 'CO/M', '+CO/M', '+CO/M, 'sub': 373', '473', '573', '373', '473', '573, '0.7*()/3>()/3'}, 'wherein changes in hydrogen and carbon monoxide chemisorption amounts depending on a temperature satisfy the following relationwherein HIM is a chemisorption amount (mol) of a hydrogen atom per total mol of M, CO/M is a chemisorption amount (mol) of carbon monoxide per total mol of M, and subscripts represent adsorption temperatures (K).2. The hydrogen spillover-based catalyst of claim 1 , wherein the silica/alumina molar ratio of zeolite is 1˜2.3. The hydrogen spillover-based catalyst of claim 1 , wherein upon partial or full structural collapse of zeolite claim 1 , an XRD (X-ray Diffraction) pattern of the catalyst shows the following:{'br': None, 'i': P', 'P, 'sub': zeolite)>(Main', 'collapse, '0.8(Main)'}{'sub': zeolite', 'collapse, 'wherein MainPis a area of the highest peak among XRD peaks of zeolite before collapse, and MainPis a base area of an XRD peak at the same 28 of zeolite after collapse.'}4. The hydrogen spillover-based catalyst of claim 1 , wherein the hydrogen activation metal is any one or more selected from the group consisting of Groups IB claim 1 , VIIB and VIII metals on a periodic table.5. The hydrogen spillover-based catalyst of claim 1 , wherein the ...

HYDRODESULFURIZATION CATALYST FOR DIESEL OIL AND HYDROTREATING METHOD FOR DIESEL OIL

A hydrodesulfurization catalyst supports one or more metals selected from elements in Group 6 of the Periodic table, one or more metals selected from elements in Group 9 or Group 10 of the same, phosphorus, and an organic acid on a composite oxide support having a specific content of both alumina and HY zeolite having a specific crystallite size. The catalyst includes 10% to 40% by mass of the Group 6 metal, 1% to 15% by mass of the Group 9 or Group 10 metal, and 1.5% to 8% by mass of phosphorus in terms of an oxide based on the catalyst. The catalyst includes 0.8% to 7% by mass of carbon derived from an organic acid and for 1 mole of the Group 9 or Group 10 element metal in terms of an element based on the catalyst, and includes 0.2 to 1.2 moles of the organic acid. 1. A hydrodesulfurization catalyst for diesel oil which supports one or more metals selected from the group consisting of elements in Group 6 of the long periodic table , one or more metals selected from the group consisting of elements in Group 9 or 10 of the long periodic table , phosphorus , and an organic acid on a composite oxide support containing 80% by mass to 99.5% by mass of alumina , and 0.5% by mass to 20% by mass of HY zeolite , the catalyst comprising:10% by mass to 40% by mass of one or more metals selected from the group consisting of elements in Group 6 in terms of an oxide based on the catalyst;1% by mass to 15% by mass of one or more metals selected from the group consisting of elements in Group 9 or 10 in terms of an oxide based on the catalyst;1.5% by mass to 8% by mass of phosphorus in terms of an oxide based on the catalyst;0.8% by mass to 7% by mass of carbon derived from the organic acid in terms of an element based on the catalyst; and0.2 moles to 1.2 moles of the organic acid per 1 mole of one or more metals selected from the group consisting of elements in Group 9 or 10 of the long periodic table,{'sup': 2', '2, 'wherein a specific surface area measured by a nitrogen ...

MOLYBDENUM BASED CATALYST SUPPORTED ON TITANIA-MODIFIED ZEOLITE

A supported catalyst having catalytic species including molybdenum as well as cobalt and/or vanadium as a promoter disposed on a support material containing zeolite modified with titanium dioxide. Various methods of preparing and characterizing the supported catalyst are disclosed. The utilization of the catalyst in treating a hydrocarbon feedstock containing sulfur compounds (e.g. dibenzothiophene) to produce a desulfurized hydrocarbon stream is also provided. 1: A Mo-based hydrodesulfurization catalyst , comprising:a support material comprising a titania-modified zeolite; anda catalytic material disposed on the support material,wherein:the catalytic material comprises molybdenum and at least one promoter;the support material has a weight ratio of zeolite to titania in a range of 5:1 to 25:1; andthe Mo-based hydrodesulfurization catalyst has a molybdenum content in a range of 10-25 wt % relative to a total weight of the Mo-based hydrodesulfurization catalyst.2: The Mo-based hydrodesulfurization catalyst of claim 1 , wherein the support material has a Si:Al weight ratio of 2:1 to 3:1 claim 1 , and a Si:Ti weight ratio of 3:2 to 7:1.3: The Mo-based hydrodesulfurization catalyst of claim 1 , wherein the at least one promoter comprises cobalt claim 1 , vanadium claim 1 , or both.4: The Mo-based hydrodesulfurization catalyst of claim 3 , wherein the at least one promoter comprises cobalt claim 3 , and wherein the Mo-based hydrodesulfurization catalyst has a cobalt content in a range of 1-5 wt % relative to a total weight of the Mo-based hydrodesulfurization catalyst.5: The Mo-based hydrodesulfurization catalyst of claim 3 , wherein the at least one promoter comprises vanadium claim 3 , and wherein the Mo-based hydrodesulfurization catalyst has a vanadium content in a range of 0.5-4 wt % relative to a total weight of the Mo-based hydrodesulfurization catalyst.6: The Mo-based hydrodesulfurization catalyst of claim 3 , wherein the at least one promoter comprises cobalt and ...

Methods and apparatuses for hydroprocessing hydrocarbons

Methods and apparatuses for hydroprocessing a hydrocarbon stream are provided herein. In an embodiment, a method of hydroprocessing the hydrocarbon stream includes hydrocracking the hydrocarbon stream in a first hydrocracking stage in the presence of a first hydrocracking catalyst to produce a first conversion stream. Components from the first conversion stream are treated in a downstream processing stage in the presence of a downstream resid hydrotreating catalyst to produce a second conversion stream.

CATALYST CONTAINING METAL CLUSTER IN STRUCTURALLY COLLAPSED ZEOLITE, AND USE THEREOF

This invention relates to a hydrogen spillover-based catalyst and use thereof, wherein a hydrogen activation metal cluster is dispersed in the form of being encapsulated in a crystalline or amorphous aluminosilicate matrix which is partially or fully structurally collapsed zeolite, thereby exhibiting high hydroprocessing or dehydrogenation activity and suppressed C-C hydrogenolysis activity. 18-. (canceled)9. A method of preparing a hydrogen spillover based catalyst , comprising:{'sup': '-', '(a) providing zeolite containing a hydrogen activation metal (M) cluster therein and having a silica/alumina molar ratio oc 2 or is less;'}{'sub': '4', 'sup': '+', '(b) ion-exchanging the zeolite with an ammonium ion (NH); and'}(c) thermally treating the ion-exchanged zeolite to thus partially or fully collapse a zeolite framework so that the hydrogen activation metal cluster is encapsulated in crystalline or amorphous aluminosilicate,wherein changes in hydrogen and carbon monoxide chemisorption amounts depending on a temperature satisfy the following relation:{'sub': 373', '473', '573', '373', '473', '575, '0.7*(H/M+H/M+H/M)/3>(CO/M+CO/M+CO/M)/3'}wherein H/M is a chemisorption amount (mol) of a hydrogen atom per total mol of given CO/M is a chemisorption amount (mol) of carbon monoxide per total mol of M., and subscripts represent adsorption temperatures (K).10. The method of claim 9 , wherein the zeolite is P-type zeolite claim 9 , A-type zeolite or X-type zeolite.11. The method of claim 9 , wherein the (a) comprises performing hydrothermal synthesis from a zeolite synthesis reaction mixture containing a hydrogen activation metal (M) precursor and having the following composition represented relative to oxides:{'sub': 2', '2', '3, 'SiO/AlO: 1˜20'}{'sub': 2', '2, 'HO/M′O: 10˜120'}{'sub': 2', '2, 'M′O/SiO: 0.38˜3, and'}{'sub': '2', 'OH/SiO: 0.76˜6,'}wherein M′ is an alkali metal.12. The method of claim 11 , wherein M′ is sodium.13. The method of claim 11 , further comprising ...

HYDRODESULFURIZATION CATALYST AND A METHOD OF PRODUCING THEREOF

A single-pot method of producing a hydrodesulfurization catalyst by hydrothermally treating a hydrothermal precursor that includes a silica source, a structural directing surfactant, an aqueous acid solution, and metal precursors that contain active catalyst materials is provided. The hydrodesulfurization catalyst includes a catalyst support having SBA-15 and preferably titanium, wherein the active catalyst materials are homogenously deposited on the catalyst support. Various embodiments of said method and the hydrodesulfurization catalyst are also provided. 1: A method of producing a hydrodesulfurization catalyst , comprising:hydrothermally treating a hydrothermal precursor comprising a silica source, a structural directing surfactant, an aqueous acid solution, a first metal precursor, and a second metal precursor, to form the hydrodesulfurization catalyst,wherein each of the first and the second metal precursors comprises an active catalyst material selected from groups 4 to 12 of the periodic table, andwherein the hydrodesulfurization catalyst comprises at least two active catalyst materials deposited on a catalyst support comprising SBA-15.2: The method of claim 1 , further comprising:calcining the hydrodesulfurization catalyst at a temperature in the range of 200 to 650° C.3: The method of claim 2 , wherein the hydrodesulfurization catalyst is calcined at a temperature in the range of 250 to 350° C. for 2 to 12 hours.4: The method of claim 1 , wherein the hydrothermal precursor further comprises a titanium source claim 1 , and wherein the catalyst support further comprises titanium.5: The method of claim 1 , wherein the hydrothermal precursor does not include a complexing agent.6: The method of claim 1 , wherein the hydrothermal precursor further comprises a complexing agent comprising citric acid.7: The method of claim 1 ,wherein the first metal precursor comprises an active catalyst material selected from nickel and cobalt, andwherein the second metal ...

CATALYTIC CRACKING GASOLINE PREHYDROGENATION METHOD

The invention relates to a catalytic cracking gasoline prehydrogenation method. Thiol etherification and double bond isomerization reactions are carried out on catalytic cracking gasoline through a prehydrogenation reactor. The reaction conditions are as follows: the reaction temperature is between 80° C. and 160° C., the reaction pressure is between 1 MPa and 5 MPa, the liquid-volume hourly space velocity is from 1 to 10 h, and the hydrogen-oil volume ratio is (3-8):1; a prehydrogenation catalyst comprises a carrier and active ingredients, the carrier contains an aluminium oxide composite carrier with a macroporous structure and one or more of ZSM-5, ZSM-11, ZSM-12, ZSM-35, mordenite, amorphous form aluminum silicon, SAPO-11, MCM-22, a Y molecular sieve and a beta molecular sieve, the surface of the carrier is loaded with one or more of the active ingredients cobalt, molybdenum, nickel and tungsten; based on oxides, the content of the active ingredients is between 0.1% and 15.5%. 1. A catalytic cracking gasoline prehydrogenation method , wherein thiol etherification and double bond isomerization reactions are carried out on catalytic cracking gasoline through a prehydrogenation reactor , and the reaction conditions are as follows: the reaction temperature is between 80° C. and 160° C. , the reaction pressure is between 1 MPa and 5 MPa , the liquid-volume hourly space velocity is from 1 to 10 h , and the hydrogen-oil volume ratio is (3-8):1; a prehydrogenation catalyst comprises a carrier and active ingredients , the carrier contains an aluminium oxide composite carrier with a macroporous structure and one or more of ZSM-5 , ZSM-11 , ZSM-12 , ZSM-35 , mordenite , amorphous form aluminum silicon , SAPO-11 , MCM-22 , a Y molecular sieve and a beta molecular sieve; the alumina composite carrier contains 0.1-12 wt % of tungsten-doped lanthanum ferrite , the mesopores of the alumina composite carrier account for 1-85% of the total pores , and the macropores of the ...

SEQUENTIAL IMPREGNATION FOR NOBLE METAL ALLOY FORMATION

Methods are provided for forming noble metal catalysts comprising both platinum and a second Group VIII metal, such as palladium, with improved aromatic saturation activity. Instead of impregnating a catalyst with both platinum and another Group VIII metal at the same time, a sequential impregnation can be used, with the Group VIII metal being impregnated prior to platinum. It has been discovered that by forming a Group VIII metal-impregnated catalyst first, and then impregnating with platinum, the distribution of platinum throughout the catalyst can be improved. The improved distribution of platinum can result in a catalyst with enhanced aromatic saturation activity relative to a catalyst with a similar composition formed by simultaneous impregnation. 19.-. (canceled)10. A supported catalyst comprising:a support comprising at least one of a zeolitic support and a mesoporous support, the support having an Alpha value of at least 100; and0.1 wt % to 5.0 wt %, based on a weight of the supported catalyst, of a combined amount of platinum and Group VIII metal on the support, a weight ratio of platinum and Group VIII metal being from 0.1 to 10, the Group VIII metal comprising Pd, Ni, Rh, Ir, Ru, Co, or a combination thereof,wherein the supported catalyst has a catalyst width and an average platinum content per volume, and wherein a peak platinum content per volume across the catalyst width differs from the average platinum content per volume by less than 100% of the average platinum content per volume.11. The supported catalyst of claim 10 , wherein the supported catalyst has an average combined platinum and Group VIII metal content per volume claim 10 , and wherein a peak combined platinum and Group VIII metal content per volume across the catalyst width differs from the average combined platinum and Group VIII metal content per volume by less than 100% of the average combined platinum and Group VIII metal content per volume.12. The supported catalyst of claim 10 , ...

STRUCTURED CATALYST FOR HYDRODESULFURIZATION, HYDRODESULFURIZATION DEVICE INCLUDING THE STRUCTURED CATALYST, AND METHOD FOR PRODUCING STRUCTURED CATALYST FOR HYDRODESULFURIZATION

Provided is a structured catalyst for hydrodesulfurization that suppresses the decline in catalytic activity and achieves efficient hydrodesulfurization. The structured catalyst for hydrodesulfurization () includes a support () of a porous structure composed of a zeolite-type compound, and at least one catalytic substance () present in the support (), the support () having channels () connecting with each other, and the catalytic substance () being present at least in the channels () of the support (). 1. A structured catalyst for hydrodesulfurization , comprising:a support of a porous structure composed of a zeolite-type compound; andat least one catalytic substance present in the support,the support comprising channels connecting with each other, andthe catalytic substance being present at least in the channels of the support,wherein the channels have any one of a one-dimensional pore, a two-dimensional pore, and a three-dimensional pore defined by a framework of the zeolite-type compound and an enlarged pore portion that is different from any of the one-dimensional pore, the two-dimensional pore, and the three-dimensional pore,the catalytic substance is present at least in the enlarged pore portion, andthe catalytic substance is made of metal oxide nanoparticles.2. The structured catalyst for hydrodesulfurization according to claim 1 , wherein the enlarged pore portion connects a plurality of pores constituting any one of the one-dimensional pore claim 1 , the two-dimensional pore claim 1 , and the three-dimensional pore with each other.3. The structured catalyst for hydrodesulfurization according to claim 1 , wherein the metal oxide nanoparticles include a metal oxide composed of at least one of nickel claim 1 , cobalt claim 1 , molybdenum claim 1 , and tungsten.4. The structured catalyst for hydrodesulfurization according to claim 3 , wherein the metal oxide nanoparticles are composed mainly of a molybdenum-based (M-Mo based) oxide and/or a tungsten-based (M-W ...

INTEGRATED PROCESS FOR SOLVENT DEASPHALTING AND GAS PHASE OXIDATIVE DESULFURIZATION OF RESIDUAL OIL

The invention is an integrated process for treating residual oil of a hydrocarbon feedstock. The oil is first subjected to solvent deasphalting then gas phase oxidative desulfurization. Additional, optional steps including hydrodesulfurization, and hydrocracking, may also be incorporated into the integrated process. 1. An integrated process for removing metals and sulfur from a residual oil feedstock , comprising:(i) deasphalting said residual oil feedstock in a first vessel, in the presence of a paraffinic solvent, to produce a gas, asphalt and deasphalted oil (DAO);(ii) separating said gas, asphalt and DAO from each other and also from said paraffinic solvent;(iii) moving said DAO to a second vessel containing an oxidative desulfurization (ODS) catalyst;{'sub': '2', '(iv) contacting said DAO and ODS catalyst with a gaseous oxidizing agent, to form SO, a second gas, and a liquid in a gaseous ODS process to remove additional sulfur in said DAO;'}(v) separating any gas and liquid produced in (iv) from each other;(vi) removing a portion of said gas of (v) from total gas, leaving a remainder;(vii) recycling said remainder to said second vessel, and;(viii) subjecting the liquid to hydrodesulfurization (HDS) with hydrogen and an HDS catalyst.2. (canceled)3. The method of claim 1 , further comprising subjecting the liquid to hydrocracking in the presence of hydrogen and a hydrocracking catalysts.4. An integrated process for removing metals and sulfur from a residual oil feedstock claim 1 , comprising:(i) deasphalting said residual oil feedstock in a first vessel, in the presence of a paraffinic solvent, to produce a gas, asphalt and a deasphalted oil (DAO);(ii) subjecting said DAO to hydrodesulfurization (HDS) in a second vessel, in the presence of an HDS catalyst, to produce a first liquid and a first;{'sub': '2', '(iii) contacting said first liquid with an ODS catalyst and a gaseous oxidizing agent to form a second gas, a second liquid product and SO;'}(iv) separating ...

CATALYST BASED ON y-KETOVALERIC ACID AND USE THEREOF IN A HYDROTREATMENT AND/OR HYDROCRACKING PROCESS

The invention relates to a catalyst comprising a support based on alumina or silica or silica-alumina, at least one element of group VIII, at least one element of group VIB and γ-ketovaleric acid. The invention also relates to the process for the preparation of said catalyst and the use thereof in a hydrotreatment and/or hydrocracking process. 1. Catalyst comprising a support based on alumina or silica or silica-alumina , at least one element of group VIII , at least one element of group VIB , and γ-ketovaleric acid.2. Catalyst according to claim 1 , in which the content of the element of group VIB is comprised between 5 and 40% by weight expressed as oxide of the metal of group VIB with respect to the total weight of the catalyst and the content of the element of group VIII is comprised between 1 and 10% by weight expressed as oxide of the metal of group VIII with respect to the total weight of the catalyst.3. Catalyst according to claim 1 , in which the molar ratio of the element of group VIII to the element of group VIB in the catalyst is between 0.1 and 0.8.4. Catalyst according to claim 1 , which additionally contains phosphorus claim 1 , the phosphorus content being comprised between 0.1 and 20% by weight expressed as POwith respect to the total weight of the catalyst and the ratio of phosphorus to the element of group VIB in the catalyst is greater than or equal to 0.05.5. Catalyst according to claim 1 , in which the content of γ-ketovaleric acid is comprised between 1 and 35% by weight with respect to the total weight of the catalyst.6. Catalyst according to claim 1 , which additionally contains an organic compound other than γ-ketovaleric acid containing oxygen and/or nitrogen and/or sulphur.7. Catalyst according to claim 6 , in which the organic compound is selected from a compound comprising one or more chemical functions selected from a carboxyl claim 6 , alcohol claim 6 , thiol claim 6 , thioether claim 6 , sulphone claim 6 , sulphoxide claim 6 , ether ...

SYSTEMS AND METHODS INCLUDING HYDROPROCESSING AND HIGH-SEVERITY FLUIDIZED CATALYTIC CRACKING FOR PROCESSING PETROLEUM-BASED MATERIALS

According to at least one aspect of the present disclosure, a method for processing a heavy oil includes introducing the heavy oil to a hydroprocessing unit, the hydroprocessing unit being operable to hydroprocess the heavy oil to form a hydroprocessed effluent by contacting the heavy oil feed with an HDM catalyst, an HDS catalyst, and an HDA catalyst. The hydroprocessed effluent is passed directly to a HS-FCC unit, the HS-FCC unit being operable to crack the hydroprocessed effluent to form a cracked effluent comprising at least one product. The cracked effluent is passed out of the HS-FCC unit. The heavy oil has an API gravity of from 25 degrees to 50 degrees and at least 20 wt. % of the hydroprocessed effluent passed to the HS-FCC unit has a boiling point less than 225 degrees ° C. 1. A system for processing a heavy oil , the system comprising:a heavy oil source;a hydroprocessing unit, the hydroprocessing unit including a hydrodemetalization (HDM) catalyst, a hydrodesulfurization (HDS) catalyst, and a hydrodearomatization (HDA) catalyst; anda high-severity fluidized catalytic cracking (HS-FCC) unit,in which an outlet of the heavy oil source is in direct fluid communication with an inlet of the hydroprocessing unit and an outlet of the hydroprocessing unit is in direct fluid communication with an inlet of the HS-FCC unit.2. The system of claim 1 , in which the hydroprocessing unit comprises two or more catalyst beds arranged in series.3. The system of claim 1 , in which the hydroprocessing unit comprises a plurality of packed red reaction zones arranged in series in a hydroprocessing reactor.4. The system of claim 1 , in which the hydroprocessing unit comprises an HDM reaction zone comprising the HDM catalyst; an HDS reaction zone comprising the HDS catalyst; and an HDA reaction zone comprising the HDA catalyst.5. The system of claim 4 , in which the HDS reaction zone is downstream of the HDM reaction zone; and the HDA reaction zone is downstream of the HDS ...

PROCESS FOR IMPROVING GASOLINE QUALITY FROM CRACKED NAPHTHA

A method is provided for producing gasoline that includes separating a cracked naphtha feed into a light catalytic naphtha fraction and a heavy naphtha fraction; and exposing the light catalytic naphtha fraction to a catalyst under effective conversion conditions to reduce sulfur content of the light catalytic naphtha fraction while also reducing a Reid vapor pressure and an olefin content of the light catalytic naphtha fraction, wherein the effective conversion conditions comprise a pressure of less than about 500 psig and a temperature of at least about 550° F. (288° C.). 1. A method for producing gasoline comprising:separating a cracked naphtha feed into a light catalytic naphtha fraction and a heavy naphtha fraction; andexposing the light catalytic naphtha fraction to a catalyst under effective conversion conditions to reduce sulfur content of the light catalytic naphtha fraction while also reducing a Reid vapor pressure and an olefin content of the light catalytic naphtha fraction, wherein the effective conversion conditions comprise a pressure of less than about 500 psig and a temperature of at least about 550° F. (288° C.).2. The method of claim 1 , further comprising blending the light catalytic naphtha fraction into one or more grades of gasoline product produced by a refinery claim 1 , each of the one or more grades of gasoline product comprising gasoline boiling range hydrocarbons claim 1 , and wherein a total olefin content for the gasoline pool in a month is about 3.0 vol % or less.3. The method of claim 1 , wherein the heavy naphtha fraction comprises about 90 wt % or more of the C9+ hydrocarbons in the cracked naphtha feed.4. The method of claim 1 , wherein the light catalytic naphtha fraction comprises C5 hydrocarbons from the cracked naphtha feed.5. The method of claim 4 , wherein the light catalytic naphtha fraction further comprises C6 hydrocarbons from the cracked naphtha feed.6. The method of claim 5 , wherein the light catalytic naphtha ...

PRODUCTION OF RENEWABLE DIESEL AND PROPYLENE

Feeds containing triglycerides are processed to produce a diesel fuel product and propylene. The diesel product and propylene are generated by deoxygenating the triglyceride-containing feed using processing conditions that enhance preservation of olefins that are present in the triglycerides. The triglyceride-containing feed is processed in the presence of a catalyst containing a Group VI metal and a Group VIII non-noble metal and in the presence of CO. 1. A method for processing a biocomponent feedstock , comprising:exposing a feedstock, the feedstock comprising at least 40 wt % of a biocomponent feed containing triglycerides, to a first catalyst in the presence of hydrogen and at least 300 vppm of CO under first effective deoxygenation conditions for forming an at least partially deoxygenated effluent, the first catalyst comprising a Group VI metal and a Group VIII non-noble metal, the at least partially deoxygenated effluent having an oxygen content that is at least 40% less than an oxygen content of the feedstock;separating the at least partially deoxygenated effluent to form a gas phase effluent comprising propylene and a liquid phase effluent; andseparating at least a portion of the propylene from the gas phase effluent.2. The method of claim 1 , wherein the propylene separated from the gas phase effluent comprises at least about 0.25 wt % of propylene relative to the weight of the biocomponent feed.3. The method of claim 1 , wherein a relative weight ratio of propylene to propane in the gas phase effluent is at least about 0.25.4. The method of claim 1 , wherein the biocomponent feed comprises at least 40 wt % of triglycerides.5. The method of claim 1 , wherein the liquid phase effluent comprises at least about 10 wt % olefins.6. The method of claim 1 , wherein the liquid phase effluent has an olefin to paraffin ratio of at least about 0.03.7. The method of claim 1 , wherein the at least one Group VI metal is tungsten or molybdenum and the at least one Group ...

METHOD FOR PRODUCING METAL-CONTAINING CATALYSTS

A method for making catalyst materials is disclosed in which active metal ingredients of the final catalyst are added to a mixture for extruding the catalyst material that includes a binder, one or more precursors of one or more base metals and/or one or more noble metals, and a crystal of a zeolite. The extruded catalyst material is then pre-calcined and ion-exchanged and then a final calcining step is applied. The catalyst materials made by such a method are also disclosed as is a method for treating a hydrocarbon stream using the catalysts. 1. A method for producing a catalyst material comprising:mixing a binder, a porous crystalline material, water, and one or more precursors of a first base metal that is Ni or Co or a mixture of these, and one or more precursors of a second base metal that is Mo or W, or a mixture of these, to form an extrudable paste;extruding the paste to form a green catalyst extrudate, drying the green catalyst extrudate to remove water, and pre-calcining the green catalyst extrudate in a nitrogen atmosphere to form a pre-calcined extrudate catalyst material;ion-exchanging the pre-calcined extrudate to obtain an ion-exchanged extrudate; andcalcining the ion-exchanged extrudate to obtain a catalyst material.2. The method of claim 1 , in which the mixing step further comprises one or more precursors of one or more noble metals Pt or Pd claim 1 , or a mixture of both.3. The method of claim 1 , in which the porous crystalline material is ZSM-48 claim 1 , ZSM-5 claim 1 , ZSM-11 claim 1 , ZSM-22 claim 1 , ZSM-23 claim 1 , ZSM-35 claim 1 , ZSM-50 claim 1 , ZSM-57 claim 1 , ZSM-58 claim 1 , zeolite beta claim 1 , mordenite claim 1 , MCM-68 claim 1 , a MCM-22 family material claim 1 , or MCM-41 claim 1 , or a mixture of two or more thereof.4. The method of claim 2 , in which the porous crystalline material is ZSM-48 claim 2 , ZSM-5 claim 2 , ZSM-11 claim 2 , ZSM-22 claim 2 , ZSM-23 claim 2 , ZSM-35 claim 2 , ZSM-50 claim 2 , ZSM-57 claim 2 , ZSM-58 ...

COMPOSITION AND A METHOD OF MAKING AND USE OF SUCH COMPOSITION

A composition and method of making such a composition that has application in the hydroprocessing of hydrocarbon feedstocks. The method comprises selecting an organic additive by the use of a correlation model for predicting catalytic activity as a function of a physical property that is associated with the organic additive and incorporating the organic additive into a support material to provide the additive impregnated composition. 1. A composition for use in the hydroprocessing of a hydrocarbon feedstock , wherein said composition comprises: a support material having incorporated therein a metal component and an organic additive selected by the use of a correlation model , wherein said correlation model provides for estimating a predicted catalytic activity of said composition that has been prepared with said organic additive having a characteristic complexation energy , and wherein said organic additive is selected from a group consisting of amide compounds , amine compounds , nitrile compounds , pyrrolidone compounds , urea compounds , and oxalate compounds , wherein said organic additive is capable of forming a metal complex with a transition metal , and wherein said organic additive has said complexation energy of an absolute value of greater than 470 kcal/mol.2. A composition as recited in claim 1 , wherein said metal component is selected from the group of Group 9 or Group 10 metals consisting of cobalt and nickel present in said composition in an amount in the range of from 0.5 wt. % to 20 wt. % claim 1 , and the group of Group 6 metals consisting of molybdenum and tungsten present in said composition in an amount in the range of from 5 wt. % to 50 wt. % claim 1 , wherein the weight percents are based on the weight of the dry support material with the metal component as the elemental form regardless of its actual form.3. A composition as recited in claim 2 , wherein said support material a porous refractory oxide selected from the group of refractory ...

CATALYTIC SYSTEM, PROCESS FOR THE PREPARATION OF SAID SYSTEM AND HYDROTREATMENT PROCESS USING SAID SYSTEM

The catalytic system comprising a nucleus containing a supported hydrotreatment, hydrogenation and/or cracking catalyst or a carrier selected from an amorphous silico-aluminate, a crystalline silico-aluminate and/or an alumina characterized in that the surface of said nucleus is partially or totally covered by a layer of molybdenite. The relative preparation process can be carried out starting from the nucleus containing the supported catalyst or carrier, depositing, on the surface of said nucleus, a molybdenite either preformed or generated in situ following the addition of an oil-soluble precursor of molybdenum so as to partially or totally cover it with a layer of molybdenite. 1. A catalytic system comprising a nucleus containing a supported hydrotreatment , hydrogenation and/or cracking catalyst or a carrier selected from an amorphous silico-aluminate , a crystalline silico-aluminate (zeolite) and/or an alumina characterized in that the surface of said nucleus is partially or totally covered by a layer of molybdenite.2. The catalytic system according to claim 1 , wherein the molybdenum contained in the molybdenite has a weight content not higher than 1% of the catalytic system.3. The catalytic system according to claim 1 , wherein the layer of molybdenite has a thickness ranging from 0.001μ to 1μ.4. The catalytic system according to claim 3 , wherein the layer of molybdenite has a thickness ranging from 0.01μ to 0.1μ.5. The catalytic system according to claim 1 , wherein the surface of the catalyst is covered by a layer of molybdenite in a percentage ranging from 10% to 100% with respect to the whole surface.6. The catalytic system according to claim 5 , wherein the surface of the catalyst is covered by a layer of molybdenite in a percentage ranging from 30% to 60% with respect to the whole surface.7. The catalytic system according to claim 1 , wherein the supported catalyst contains metals of group VI and VIII A.8. The catalytic system according to claim 1 , ...

SYSTEMS AND METHODS INCLUDING HYDROPROCESSING AND HIGH-SEVERITY FLUIDIZED CATALYTIC CRACKING FOR PROCESSING PETROLEUM-BASED MATERIALS

According to at least one aspect of the present disclosure, a method for processing a heavy oil includes introducing the heavy oil to a hydroprocessing unit, the hydroprocessing unit being operable to hydroprocess the heavy oil to form a hydroprocessed effluent by contacting the heavy oil feed with an HDM catalyst, an HDS catalyst, and an HDA catalyst. The hydroprocessed effluent is passed directly to a HS-FCC unit, the HS-FCC unit being operable to crack the hydroprocessed effluent to form a cracked effluent comprising at least one product. The cracked effluent is passed out of the HS-FCC unit. The heavy oil has an API gravity of from 25 degrees to 50 degrees and at least 20 wt. % of the hydroprocessed effluent passed to the HS-FCC unit has a boiling point less than 225 degrees ° C. 1. A method for processing heavy oil , the method comprising:introducing a heavy oil to a hydroprocessing unit, the hydroprocessing unit being operable to hydroprocess the heavy oil to form a hydroprocessed effluent by contacting the heavy oil with a hydrodemetalization (HDM) catalyst, a hydrodesulfurization (HDS) catalyst, and a hydrodearomatization (HDA) catalyst;passing the hydroprocessed effluent directly to a high-severity fluidized catalytic cracking (HS-FCC) unit, the HS-FCC unit being operable to contact the hydroprocessed effluent with a cracking catalyst, where at least a portion of the hydroprocessed effluent is cracked to form a cracked effluent comprising at least one product; andpassing the cracked effluent out of the HS-FCC unit,where the heavy oil has an American Petroleum Institute (API) gravity of from 25 degrees to 50 degrees and at least 20 weight percent (wt. %) of the hydroprocessed effluent passed to the HS-FCC unit has a boiling point less than 225 degrees Celsius (° C.).2. The method of claim 1 , in which the heavy oil comprises crude oil.3. The method of claim 1 , further comprising passing the cracked effluent to a separation unit operable to separate the ...

IN SITU BIFUNCTIONAL CATALYST FOR DEEP DESULFURIZATION AND INCREASING OCTANE NUMBER OF GASOLINE AND PREPARATION METHOD THEREOF

Provided are an in situ bifunctional catalyst for deep desulfurization and increasing octane number of gasoline, and its preparation method and application. The bifunctional catalyst includes a modified catalyst carrier and a loaded active metal, where the modified catalyst carrier is a composite carrier prepared through mixing γ-AlOand an acidic molecular sieve by a binder and calcining. When the bifunctional catalyst provided by the present application is used for hydrodesulfurization of gasolines, deep desulfurization, olefin reduction and octane number preservation can be realized simultaneously, thereby obtaining a high-quality oil product. 1. A bifunctional catalyst for hydrodesulfurization coupled with isomerization , comprising a modified catalyst carrier and a loaded active metal , wherein the modified catalyst carrier is a composite carrier prepared by mixing γ-AlOand an acidic molecular sieve by a binder and calcining.2. The bifunctional catalyst according to claim 1 , wherein a mass ratio of γ-AlOto the acidic molecular sieve is (1-9):1; and/or claim 1 , the acidic molecule sieve is selected from one or more of ZSM-5 claim 1 , MCM-41 claim 1 , SAPO-34 and Bata molecular sieve.3. The bifunctional catalyst according to claim 1 , wherein the active metal is selected from two or more of VIB Group and VIII Group elements in the Periodic Table of Elements.4. The bifunctional catalyst according to claim 1 , wherein the catalyst for hydrodesulfurization is obtained by loading an active metal onto the modified catalyst carrier via an impregnation method claim 1 , then aging claim 1 , drying claim 1 , and calcining.5. A preparation method of the bifunctional catalyst for hydrodesulfurization coupled with isomerization according to claim 1 , comprising:{'sub': 2', '3, 'mixing γ-AlOand an acidic molecular sieve by a binder and calcining, to prepare a modified catalyst carrier; and'}loading an impregnation solution containing an active metal onto the modified ...

BIFUNCTIONAL CATALYST FOR DEEP DESULFURIZATION AND GASOLINE QUALITY IMPROVEMENT AND PREPARATION METHOD THEREFOR

Provided are a bifunctional catalyst for deep desulfurization and gasoline quality improvement and a preparation method therefore and a use thereof. The bifunctional catalyst includes a modified catalyst and a loaded active metal, where the modified catalyst carrier is a γ-AlOmodified with a rare earth element, or the modified catalyst carrier is a composite carrier prepared by mixing and calcinating γ-AlOand an acid molecular sieve through a binder, and then modifying with the rare earth element. The bifunctional catalyst for deep desulfurization and gasoline quality improvement can achieve deep desulfurization of high-sulfur fluid catalytic cracking gasoline, and ensure no significant loss of octane number under relatively mild conditions.

SILICA CONTAINING ALUMINA SUPPORTS, CATALYSTS MADE THEREFROM AND PROCESSES USING THE SAME

Alumina support compositions comprising at least 0.1 wt % of silica are disclosed. The alumina support are characterized by a pore volume of greater than 0.60 cc/g, a median pore size ranging from about 70 to about 120, a pore size distribution such that at least 90% of the total pore volume falls within the range of about 20 to about 250, and a pore size distribution width of no less than about 40. Alumina compositions of the present invention exhibit a primary peak mode at a pore diameter less than the median pore diameter. Also provided are catalysts made from the alumina supports, and processes of preparing and using the supports and catalysts. 1. An alumina composition which comprises a precipitated alumina comprising at least about 0.1 wt % silica , said composition having a pore volume of about 0.60 cc/g or greater , a median pore size ranging from about 70 Å to about 120 Å , a pore size distribution such that at least about 90% of the total pore volume falls within the range of about 20 Å to about 250 Å , and a pore size distribution width of about 40 Å or greater.2. The alumina composition of claim 1 , wherein the composition comprise at least 3 wt % SiO.3. (canceled)4. The alumina composition of claim 2 , wherein the composition comprise from about 3 to about 10 wt % SiO.5. The alumina composition of claim 1 , wherein the composition has a total pore volume of about 0.60 cc/g to about 1.0 cc/g.6. The alumina composition of claim 5 , wherein the pore size distribution width ranges from about 40 Å to about 120 Å.7. The alumina composition of claim 6 , wherein from about 90 to about 95% of the total pore volume falls within the range of about 20 Å to about 250 Å.8. The alumina composition of claim 1 , wherein the pore volume and pore size distribution properties are determined by mercury penetration porosimetry using a mercury porosimeter at a pressure range from about atmospheric pressure to about 60 claim 1 ,000 psi claim 1 , with a contact angle claim 1 , ...

HIGH ACTIVITY HYDROTREATING CATALYSTS AND PROCESSES USING THE SAME

This disclosure relates to supported multi-metallic catalysts for use in the hydrotreating of hydrocarbon feeds. The catalysts are prepared from a catalyst precursor comprised of at least one Group VIB metal, at least one Group VIII metal and an organic acid. The catalyst precursor is thermally treated to partially decompose the organic acid, then sulfided. The catalysts have a high carbon-as-carboxyl to total carbon ratio (C/C) as a result of a unique post-metal calcination method employed during the manufacture of the catalyst. 1. A process for hydrotreating a hydrocarbon feedstock , comprising: contacting the feedstock with a hydrotreating catalyst under hydrotreating conditions to produce a hydrotreated effluent , wherein the hydrotreating catalyst comprises:(a) an inorganic catalyst support; and{'sub': carboxy', 'total, '(b) a partially oxidized metal-organic component; wherein the catalyst has (i) a loss-on-ignition of greater than 1 to 20 wt. % and (ii) a carbon-as-carboxyl to total residual carbon ratio (C/C) of at least 0.10 as determined by X-ray photoelectron spectroscopy.'}2. The process of claim 1 , wherein the catalyst further comprises a phosphorus component.3. The process of claim 2 , wherein the phosphorus component is present in an amount of from 1 to 10 wt. % claim 2 , based on the bulk dry weight of the catalyst claim 2 , calculated as PO.4. The process of claim 1 , wherein the inorganic catalyst support is selected from the group consisting of alumina claim 1 , silica claim 1 , and alumina-silica.5. The process of claim 1 , wherein the metal portion of the partially oxidized metal-organic component comprises at least one Group VIB metal and at least one Group VIII metal.6. The process of claim 5 , wherein the at least one Group VIB metal is Mo and the at least one Group VIII metal is Ni.7. The process of claim 1 , wherein the organic portion of the metal-organic component claim 1 , prior to partial oxidation claim 1 , is a hydroxycarboxylic acid ...

METHODS AND APPARATUSES FOR HYDROTREATING HYDROCARBONS

Methods and apparatuses are provided for hydrotreating hydrocarbons. A method includes heating a start-up oil in a stripper liquid fraction heat exchanger during a start-up period, and heating a reactor with the start-up oil. The start-up oil is discharged from the reactor when the start-up period ends, and a standard operating period begins after the start-up period. A reactor effluent is produced by introducing a hydrocarbon stream into the reactor during the standard operating period, where hydrogen sulfide is produced from an organic sulfur compound in the hydrocarbon stream. Steam is produced in the stripper liquid fraction heat exchanger during the standard operating period. 1. A method of hydrotreating hydrocarbons comprising:heating a start-up oil in a stripper liquid fraction heat exchanger during a start-up period;heating a reactor with the start-up oil during the start-up period;discharging the start-up oil from the reactor when the start-up period ends, wherein a standard operating period begins after the start-up period;feeding a hydrocarbon stream into the reactor during the standard operating period to produce hydrogen sulfide from an organic sulfur compound in the hydrocarbon stream, wherein the reactor produces a reactor effluent; andproducing steam in the stripper liquid fraction heat exchanger during the standard operating period.2. The method of further comprising:separating gases from the reactor effluent in a gas separator during the standard operating period to produce a recycle gas stream and a gas separator liquid effluent.3. The method of further comprising:fractionating the gas separator liquid effluent in a stripper during the standard operating period to produce a stripper vapor fraction stream and a stripper liquid fraction stream; andwherein producing steam in the stripper liquid fraction heat exchanger during the standard operating period comprises producing steam in the stripper liquid fraction heat exchanger from the stripper liquid ...

PRODUCTION OF DIESEL AND BASE STOCKS FROM CRUDE OIL

A process of producing Group III base oils, along with a naphtha product and diesel product, from whole waxy crude oil is provided. The inventive process omits the typical vacuum distillation stage and separations to form the typical cuts off of the vacuum tower. By selecting a waxy crude oil suitable for processing without separations, the crude oil may be hydroprocessed, dearomatized, dewaxed, and hydrofinished to produce a Group III base oil. Additionally, the dewaxing catalyst will isomerize the naphtha range molecules to increase the octane value to a suitable level for blending into gasoline and the diesel range molecules to reduce the diesel cloud point. 1. A method for producing lubricant base oils from a whole petroleum crude oil , comprising:a. providing a whole petroleum crude oil feedstock comprising less than about 2 wt % of heptane asphaltenes, less than about 2 wt % of Conradson carbon residue (CCR), and less than about 50 ppm of metals;b. hydrotreating the whole petroleum crude oil feedstock on at least one bed of a hydrotreating catalyst under effective hydrotreating conditions to produce a hydrotreated effluent having less sulfur, nitrogen and aromatics than the whole petroleum crude oil;c. dewaxing the hydrotreated effluent in the presence of a dewaxing catalyst to produce a naphtha product having an octane value greater than 60, a diesel product having a cloud point less than 0° C., and a lubricant base oil product; andd. fractionating the lubricant base oil product into at least a low viscosity lubricant base oil product having a viscosity of 2-8 cSt at 100° C. and a high viscosity lubricant base oil product having a viscosity of 6-30 cSt at 100° C.2. The method of claim 1 , wherein the low viscosity lubricant base oil product and the high viscosity lubricant base oil product have a viscosity index of at least 120 claim 1 , a pour point of about −15° C. claim 1 , and less than 300 ppm sulfur.3. The method of claim 1 , wherein the naphtha product ...

TRIM DEWAXING OF DISTILLATE FUEL

Methods and catalysts are provided for performing dewaxing of diesel boiling range fractions, such as trim dewaxing, that allow for production of diesel boiling range fuels with improved cold flow properties at desirable yields. In some aspects, the methods can include use of dewaxing catalysts based on an MEL framework structure (ZSM-11) to provide improved dewaxing activity. This can provide sufficient dewaxing activity to achieve a desired level of improvement in cold flow properties at the lower hydrotreating temperatures that are generally desired near the start of operation of a hydrotreating reactor. In other aspects, the methods can include use of MEL dewaxing catalysts with reduced ratios of molecular sieve to binder so that trim dewaxing can be provided while maintaining a desirable yield under end-of-run hydrotreating conditions. 119-. (canceled)20. A method for treating a distillate boiling range feed , comprising:exposing a distillate boiling range feed to a hydrotreating catalyst under effective hydroprocessing conditions to form a hydrotreated effluent; andexposing at least a portion of the hydrotreated effluent to a dewaxing catalyst under the effective hydroprocessing conditions to form a dewaxed effluent comprising a diesel boiling range product, the dewaxing catalyst comprising one or more hydrogenation metals supported on a bound molecular sieve having a MEL framework structure, the catalyst having a ratio of molecular sieve to binder by weight of about 1.0 or less, the effective hydroprocessing conditions comprise a temperature of at least about 370° C.21. The method of claim 20 , wherein the bound catalyst has a ratio of molecular sieve to binder by weight of about 0.8 or less.22. The method of claim 20 , wherein the effective hydroprocessing conditions comprise a temperature of at least about 380° C.23. The method of claim 20 , wherein the molecular sieve comprises ZSM-11.24. The method of claim 20 , wherein the dewaxing catalyst comprises ...

SULPHONIC ACID SALTS FOR METAL CATALYST PREPARATION

The invention relates to the preparation of catalyst precursor using an alkane-sulphonic acid metal salt, use of alkane-sulphonic acid for the preparation of catalyst precursor and the use of such a catalyst precursor in chemical reactions for the production of fine chemicals in the chemical industry, particularly in the refining industry. 2. The catalyst precursor according to claim 1 , wherein said at least one porous support is a refractory porous support chosen from among alumina claim 1 , silica claim 1 , zircon claim 1 , magnesia claim 1 , beryllium oxide claim 1 , chromium oxide claim 1 , titanium oxide claim 1 , thorium oxide claim 1 , ceramics claim 1 , carbon black claim 1 , graphite claim 1 , and activated carbon claim 1 , as well as combinations thereof.3. The catalyst precursor according to claim 1 , wherein said at least one porous support is a refractory porous support chosen from among the amorphous silicoaluminate claim 1 , crystalline silicoaluminate (zeolite) and silica-titanium oxide supports.4. The catalyst precursor according to claim 1 , wherein the at least one metal adsorbed on said support is any metal chosen from among the metals in columns 3 to 12 of the IUPAC periodic table of elements claim 1 , preferably from among the metals in columns 5 to 11 claim 1 , more preferably from among the metals in columns 5 to 10.5. The catalyst precursor according to claim 1 , wherein said at least one metal adsorbed on said support is any metal chosen from among vanadium claim 1 , niobium claim 1 , tantalum claim 1 , chromium claim 1 , molybdenum claim 1 , tungsten claim 1 , iron claim 1 , ruthenium claim 1 , osmium claim 1 , cobalt claim 1 , rhodium claim 1 , iridium claim 1 , nickel claim 1 , palladium claim 1 , platinum claim 1 , and mixtures of two or more of them in any proportions.6. The catalyst precursor according to claim 1 , wherein said at least one metal adsorbed on said support is a mixture chosen from among nickel-tungsten claim 1 , cobalt ...

NAPHTHA HYDRODESULFURIZATION

Methods are provided for performing selective hydrodesulfurization on a naphtha boiling range stream naphtha boiling range portion of a feed. It has been unexpectedly discovered that hydrodesulfurization with improved octane retention can be performed by using a catalyst that comprises CoMo supported on a catalyst support that includes a zeotype framework. By using a catalyst support including a zeotype framework, an unexpectedly high amount of octane in the naphtha boiling range portion of the hydrodesulfurized effluent is maintained. 1. A method for performing naphtha hydrodesulfurization , comprising:sulfiding a hydrotreating catalyst comprising 1.5 wt % to 4.0 wt % cobalt oxide and 5.0 wt % to 15 wt % molybdenum oxide, relative to a weight of the hydrotreating catalyst, an organic dispersion agent, and a support comprising a zeotype framework having a 10-member ring pore channel as the largest size pore channel, to form a sulfided hydrotreating catalyst; andexposing a feed comprising a naphtha boiling range portion to the sulfided hydrotreating catalyst under selective hydrodesulfurization conditions to form a hydrotreated effluent, the naphtha boiling range portion of the feed comprising 5.0 wt % or more of olefins.2. The method of claim 1 , wherein the support comprises a MEL framework claim 1 , a MRE framework claim 1 , or a combination thereof.3. The method of claim 1 , wherein the support comprises ZSM-11 claim 1 , ZSM-48 claim 1 , or a combination thereof.4. The method of claim 1 , wherein the support further comprises a binder.5. The method of claim 4 , wherein the binder comprises alumina claim 4 , silica claim 4 , titania claim 4 , zirconia claim 4 , or a combination thereof.6. The method of claim 4 , wherein the support comprises a weight ratio of zeotype framework to binder of 0.2 to 10.7. The method of claim 1 , wherein the hydrotreating catalyst comprises an average pore size of 17.0 nm or less.8. The method of claim 1 , wherein the hydrotreating ...

SELECTIVE HYDROGENATION CATALYST FOR USE IN THE TREATMENT OF ESSENCE CUTTINGS CONTAINING DIOLEFINS AND STYRENIC COMPOUNDS

On décrit un catalyseur permettant l'hydrogénation sélective des composés insaturés dioléfiniques et styréniques (en particulier le styrène) dans les essences, sans hydrogéner les composés aromatiques et monooléfiniques. Ce catalyseur comprend un support choisi parmi les oxydes réfractaires tels que les alumines, les silices, les silices-alumines ou la magnésie, utilisés seuls ou en mélange entre eux, sur lequel sont déposés au moins un métal noble du groupe VIII, tel que le palladium, et au moins un métal du groupe VIB, tel que le molybdène et/ ou le tungstène. A catalyst is described which allows the selective hydrogenation of unsaturated diolefinic and styrenic compounds (in particular styrene) in gasolines, without hydrogenating the aromatic and monoolefinic compounds. This catalyst comprises a support chosen from refractory oxides such as aluminas, silicas, silica-aluminas or magnesia, used alone or as a mixture with one another, on which are deposited at least one noble metal from group VIII, such as palladium, and at least one metal from group VIB, such as molybdenum and / or tungsten.

Catalyst for simultaneous hydrotreating and hydrodewaxing of hydrocarbons

Waxy shale oil feeds containing organonitrogen and/or organosulfur components are contacted with a catalyst comprising a Group VIB metal component on a support containing silicalite and a porous refractory oxide under conditions of elevated temperature and pressure and in the presence of hydrogen so as to simultaneously reduce its pour point and its organosulfur and/or organonitrogen content.

Process for simultaneous hydrotreating and hydrodewaxing of hydrocarbons

Waxy shale oil feeds containing organonitrogen and/or organosulfur components are contacted with a catalyst comprising a Group VIB metal component on a support containing silicalite and a porous refractory oxide under conditions of elevated temperature and pressure and in the presence of hydrogen so as to simultaneously reduce its pour point and its organosulfur and/or organonitrogen content.

Catalyst for simultaneous hydrotreating and hydrodewaxing of hydrocarbons

A catalyst, of especial usefulness in simultaneously reducing the pour point and the organosulfur and/or organonitrogen content of waxy shale oils, comprises a Group VIB metal component on a support comprising a porous refractory oxide and a crystalline silica, such as silicalite.

Catalyseur d'hydrogenation selective utilisable pour le traitement des coupes essences contenant des diolefines et des composes styreniques

Extremely low acidity USY and homogeneous, amorphous silica-alumina hydrocracking catalyst and process

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. 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.

Catalysts Having Metal Clusters Encapsulated in Structurally Collapsed Zeolite and Use Thereof

본 발명의 구체예에서는 제올라이트 구조가 부분적으로 또는 전체적으로 붕괴된 결정질 또는 비결정질 알루미노실리케이트 매트릭스 내에 수소 활성화 금속 클러스터가 둘러싸인 형태로 분산됨으로써 높은 수소화 또는 탈수소화 반응 활성 및 억제된 C-C 수소화분해 활성을 나타내는 수소의 스필오버-기반 촉매 및 이의 용도가 개시된다. In an embodiment of the present invention, hydrogen exhibiting high hydrogenation or dehydrogenation activity and suppressed CC hydrocracking activity by dispersing in a form surrounded by hydrogen-activated metal clusters in a crystalline or amorphous aluminosilicate matrix in which the zeolite structure partially or completely collapsed. Spillover-based catalysts and uses thereof are disclosed.

Deparaffination method and catalyst for carrying out said method

FIELD: chemistry. SUBSTANCE: described is a method for deparaffination of hydrocarbon material containing a waxy component by isomerising said component, which involves bringing the material, in deparaffination conditions, into contact with a catalyst system containing ZSM-48 and a molecular sieve with an MTT structure, where the ZSM-48 has molar ratio of silicon oxide to aluminium oxide of 100, the molecular sieve with an MTT structure has molar ratio of silicon oxide to aluminium oxide of less than 45, the molar sieve with an MTT structure is ZSM-23, and the ratio of ZSM-48 to ZSM-23 is at least 75:25. EFFECT: high efficiency of the process. 16 cl, 2 dwg, 3 tbl, 6 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 501 843 (13) C2 (51) МПК C10G 45/64 (2006.01) B01J 29/80 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2011127673/04, 15.12.2009 (24) Дата начала отсчета срока действия патента: 15.12.2009 (72) Автор(ы): ЭЛИА Кристин Н. (US), ЛАИ Веньих Ф. (US) (43) Дата публикации заявки: 27.01.2013 Бюл. № 3 C 2 2 5 0 1 8 4 3 R U C 2 (56) Список документов, цитированных в отчете о поиске: US 6051129 А, 18.04.2000. US 20070138060 А1, 21.06.2007. US 20070155614 A1, 05.07.2007. US 20040067843 A1, 08.04.2004. US 4906350 A, 06.03.1990. WO 2004033096 A1, 22.04.2004. RU 2177468 C2, 27.12.2001. RU 2211855 C2, 10.09.2003. WO 2005083039 A1, 09.09.2005. WO 2004033594 A1, 22.01.2004. US 20040065584 A1, 08.04.2004. US 20040065582 A1, 08.04.2004. (см. прод.) (85) Дата начала рассмотрения заявки PCT на национальной фазе: 18.07.2011 (86) Заявка PCT: US 2009/006563 (15.12.2009) (87) Публикация заявки РСТ: WO 2010/077308 (08.07.2010) Адрес для переписки: 191036, Санкт-Петербург, а/я 24, "НЕВИНПАТ" (54) СПОСОБ ДЕПАРАФИНИЗАЦИИ И КАТАЛИЗАТОР ДЛЯ ЕЕ ПРОВЕДЕНИЯ (57) Реферат: Изобретение относится к области катализа. Описан способ депарафинизации содержащего низкозастывающий компонент углеводородного сырья путем изомеризации указанного ...

一种介孔Zn-ZSM-5分子筛及低成本制备方法

本发明涉及一种介孔Zn‑ZSM‑5分子筛及低成本制备方法，介孔孔径集中在5‑30 nm，比表面积为300‑600 m 2 /g；氧化锌含量为分子筛总重量的0.1~10 wt%。介孔Zn‑ZSM‑5分子筛的酸强度低，Zn的分散性好，抗积碳性能强，所述介孔Zn‑ZSM‑5分子筛可以用于加氢裂化、催化裂化、烃类异构化等领域。

核壳结构的纳米单晶ZSM‑5@Silicalite‑1分子筛及其制备方法

本发明涉及一种核壳结构的纳米单晶ZSM‑5@Silicalite‑1分子筛及其制备方法。本发明以纳米ZSM‑5分子筛为核相，晶粒尺寸为50～800nm，以纳米Silicalite‑1分子筛为壳相，壳层厚度为5～100nm；采用弱酸性溶液对核相ZSM‑5分子筛外表面进行预处理后，在壳层分子筛生长液体系中进行水热晶化，制得含致密壳层的纳米单晶ZSM‑5@Silicalite‑1分子筛。本发明提供的分子筛具有连续的孔道、扩散阻力小、一体化机械强度高、选择性高的特点；此外，其可以有效用于催化裂化汽油加氢改质过程中，且在芳烃择形歧化、择形烷基化、择形异构化及催化裂化汽油加氢改质等方面具有优异的催化性能。

加氢催化剂及其制备方法和应用

本发明涉及加氢催化剂技术领域，公开了一种加氢催化剂及其制备方法和应用，该催化剂包括载体和负载在所述载体上的加氢活性金属组分，所述加氢活性金属组分含有至少一种VIB族金属组分以及至少一种VIII族金属组分，所述载体为含磷氧化铝；该加氢催化剂经漫反射紫外可见光谱(DRUVS)测量时，630nm与500nm处的吸光度分别为F 630 和F 500 ，且二者的比值Q＝F 630 /F 500 为1‑3；VIB族金属组分的分布因子σ VIB (R)为0.5‑3.5；VIII族金属组分的分布因子σ VIII (R)为0.5‑3.5。与现有技术相比，本发明的加氢催化剂在应用于加氢处理时，具有优异的杂原子脱除效果，且具有优异的稳定性。

一种选择性加氢脱硫催化剂和脱硫方法

本发明提供一种选择性加氢脱硫催化剂和脱硫方法。本发明的选择性加氢脱硫催化剂的主体成分是以包括经金属盐处理的金属氧化物作为载体负载活性金属成分而得到；其中，所述活性金属选自周期表IA、VIII、VIB和VIIB族中的两种以上元素。此外，本发明的选择性加氢脱硫方法是对汽油原料进行萃取蒸馏并利用上述选择性加氢脱硫催化剂进行选择性加氢脱硫。本发明的脱硫方法能耗低、脱硫率高，并且脱硫汽油的辛烷值损失小。

A process for reducing sulfur and olefin contents in gasoline

본 발명은, 가솔린 공급원료와 수소를 수소화정제 촉매 및 옥탄가 회복 촉매와 접촉시키는 것을 포함하는, 가솔린의 황 및 올레핀 함량을 저감시키는 방법을 개시한다. 이 공정으로부터 얻은 유출물을 분리하여, 메르캅탄을 함유하지 않으며 황 및 올레핀의 함량이 낮으면서도 옥탄가 손실이 적은, 수소화처리된 가솔린 유분을 얻는다. 그것은 최종 가솔린 제품의 블렌딩 성분으로서 사용될 수 있으며, 최종 가솔린 제품의, 예를 들면 200 ppm 미만 정도의 낮은 황 함량, 예를 들면 20 중량% 미만 정도의 낮은 올레핀 함량, 및 낮은 옥탄가 손실에 기여할 수 있다. The present invention discloses a method for reducing the sulfur and olefin content of gasoline, comprising contacting the gasoline feedstock and hydrogen with a hydrorefining catalyst and an octane number recovery catalyst. The effluent obtained from this process is separated to obtain a hydrogenated gasoline fraction which contains no mercaptan and has low sulfur and olefin content and low loss of octane. It can be used as a blending component of the final gasoline product and can contribute to a low sulfur content, for example of less than 200 ppm, for example, a low olefin content of less than 20% by weight, and a low octane number loss of the final gasoline product. .

Катализатор гидродесульфуризации для дизельного топлива и способ гидроочистки дизельного топлива

Изобретение относится к катализатору гидродесульфуризации для дизельного топлива, в котором один или несколько металлов, выбранных из группы, состоящей из элементов Группы 6 длинной формы Периодической таблицы, один или несколько металлов, выбранных из группы, состоящей из элементов Группы 9 или 10 длинной формы Периодической таблицы, фосфор и органическая кислота нанесены на носитель на основе смешанного оксида, содержащий 80-99,5 % масс. оксида алюминия и 0,5-20 % масс. цеолита HY, причем катализатор содержит: 10-40 % масс. одного или нескольких металлов, выбранных из группы, состоящей из элементов Группы 6, в расчете на оксид, по отношению к массе катализатора; 1-15 % масс. одного или нескольких металлов, выбранных из группы, состоящей из элементов Группы 9 или 10, в расчете на оксид по отношению к массе катализатора; 1,5-8 % масс. фосфора, в расчете на оксид по отношению к массе катализатора; 0,8-7 % масс. углерода, полученного из органической кислоты, в расчете на химический элемент по отношению к массе катализатора; и 0,2-1,2 моль органической кислоты на 1 моль одного или нескольких металлов, выбранных из группы, состоящей из элементов Группы 9 или 10 длинной формы Периодической таблицы, где удельная площадь поверхности, измеренная с помощью способа адсорбции азота, составляет от 110 до 300 м 2 /г, объем пор, измеренный с помощью способа ртутной порозиметрии, составляет от 0,3 до 0,6 мл/г, средний диаметр пор, измеренный с помощью способа ртутной порозиметрии, составляет от 6,5 до 14 нм, и цеолит HY имеет (a) SiO 2 /Al 2 O 3 (молярное отношение) от 3 до 10, (b) постоянную кристаллической решетки от 2,435 до 2,465 нм, (c) молярное отношение Al в каркасе цеолита к Al в целом от 0,2 до 0,9 и (d) диаметр кристаллитов от 30 до 100 нм. Технический результат заключается в разработке технологии сверхглубокой десульфуризации для удаления по существу большей части содержания серы в дизельном топливе. 2 н. и 1 з.п. ф-лы, 5 табл., 10 пр. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) ...

Hydrodesulfurization catalyst for diesel oil and hydrotreating method for diesel oil

This catalyst of the present invention is a hydrodesulfurization catalyst that supports one or more metals selected from a group consisting of elements in Group 6 of the long period periodic table, one or more metals selected from a group consisting of elements in Group 9 or Group 10 of the same, phosphorus, and an organic acid on a composite oxide support having a specific content of both alumina and HY zeolite having a specific crystallite size and the like. The catalyst includes 10% by mass to 40% by mass of the Group 6 metal, 1% by mass to 15% by mass of the Group 9 or Group 10 metal, and 1.5% by mass to 8% by mass of phosphorus in terms of an oxide based on the catalyst. The catalyst includes 0.8% by mass to 7 % by mass of carbon derived from an organic acid and for 1 mole of the Group 9 element metal or Group 10 element metal in terms of an element based on the catalyst, and includes 0.2 moles to 1.2 moles of the organic acid. The specific surface area, pore volume, and average pore diameter in a pore distribution are within specific ranges.

Selective hydrodesulfurization catalyst

This invention relates to a catalyst and process for selectively hydrodesulfurizing naphtha feedstreams using a catalyst comprising at least one hydrodesulfurizing metal supported on a low acidity, ordered mesoporous support material.

Catalyst of deep hydrodesulfurization of vacuum gasoil and method of its preparation (variants)

FIELD: technological processes.SUBSTANCE: catalyst of deep hydrodesulfurization of vacuum gas oil contains, by weight: cobalt oxide 6–8, molybdenum oxide 18–24 and a carrier consisting of silicon oxide 6–16 and aluminum oxide-the balance, including: 20–60 % by weight of aluminum oxide in the form of boehmite, 20–40 % by weight of aluminum oxide obtained by preliminary treatment of aluminum hydroxide with a 1–5 % nitric acid solution at a solution temperature of 5–10 °C, dried by spraying in a stream of hot air, and 20–40 % by weight of aluminum oxide in the form of mesoporous aluminosilicate. Two variants of a method of a catalyst of deep hydrodesulfurization of a vacuum gas oil preparation are described. One of the variants of the method includes the steps where the resulting mixture is: suspended, peptized, molybdenum oxide is added, triethylene glycol is added, stirring until a homogeneous mass is obtained, the granules are extruded, the extrudates are dried and calcined, then impregnated with an aqueous solution of cobalt nitrate.EFFECT: use of the suggested catalyst makes it possible to increase the catalytic activity in hydrodesulfurization reactions, as well as to increase the mechanical strength.3 cl, 2 tbl, 6 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) (19) RU (11) (13) 2 666 733 C1 (51) МПК B01J 23/882 (2006.01) B01J 21/12 (2006.01) B01J 29/06 (2006.01) B01J 37/04 (2006.01) B01J 37/08 (2006.01) C10G 45/08 (2006.01) C10G 45/12 (2006.01) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 45/08 (2018.05); C10G 45/12 (2018.05); B01J 23/882 (2018.05); B01J 21/12 (2018.05); B01J 37/04 (2018.05); B01J 37/08 (2018.05); B01J 29/06 (2018.05) (21)(22) Заявка: 2018108867, 13.03.2018 13.03.2018 Дата регистрации: 12.09.2018 (45) Опубликовано: 12.09.2018 Бюл. № 26 2 6 6 6 7 3 3 R U (56) Список документов, цитированных в отчете о поиске: SU 1297899 A1, 23.03.1987. SU 1162479 A, 23.06.1985. RU 2620267 C1, 24.05.2017. US 4179410 A1, 18.12. ...

Process

Method of producing a catalyst for isodeparaffinization of diesel oil fractions

FIELD: technological processes. SUBSTANCE: preparing a molded zeolite-containing catalyst support based on a mixture of an acid component – zeolite of the *MRE structure, which is EU-2, having a molar ratio of SiO 2 :Al 2 O 3 =160÷200, and aluminum oxide with BET specific surface area of at least 250 m 2 /g. Prior to mixing, zeolite is pre-treated in conditions which do not lead to amorphization and do not lead to loss of micropores of the zeolite. Mixture is moistened, peptized, plasticizer is introduced, molded, dried and calcined. Platinum is deposited on the obtained support by ion exchange from an impregnating solution containing Pt(NH 3 ) 2 (NO 2 ) 2 , successively holding carrier at room temperature for at least 3 hours, at temperature 80–95 °C for at least 5 hours, then at room temperature for at least 12 hours. Impregnated catalyst is dried at stepped rise of temperature (60, 80, 120 °C) and holding at each temperature for two, four and four hours respectively. Dried catalyst calcined at temperature of 400–450 °C for 2–3 hours. EFFECT: technical result consists in improvement of output of target dewaxed products on isodeparaffinization catalyst using gas-raw mixture with sulfur content of up to 5000 mg/kg. 4 cl, 2 dwg, 4 tbl, 4 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 37/30 B01J 29/74 C10G 45/64 C10G 45/12 (11) (13) 2 734 969 C1 (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 37/0036 (2020.05); B01J 29/703 (2020.05); B01J 37/30 (2020.05); C10G 45/12 (2020.05); C10G 45/64 (2020.05) (21)(22) Заявка: 2020103041, 24.01.2020 24.01.2020 Дата регистрации: 26.10.2020 (45) Опубликовано: 26.10.2020 Бюл. № 30 2 7 3 4 9 6 9 R U (56) Список документов, цитированных в отчете о поиске: Miao Zhai, Liyuan Li, Yulei Ba, Kake Zhu, Xinggui Zhou. Fabricating ZSM-23 with Reduced Aspect Ratio Through Ball-Milling and Recrystallization: Synthesis, Structure and Catalytic Performance ...

Gasoline with sulfur and mercaptans small amount production method

FIELD: technological processes.SUBSTANCE: invention relates to the sulfur compounds and olefins containing gasoline processing method, wherein the method comprises comprising at least the following steps: a) reacting, at least in one reactor, of gasoline, hydrogen and hydrodesulfurization catalyst at temperature from 270 to 400 °C, pressure from 0.5 to 5 MPa, volume velocity of 0.5 to 20 hand expressed in normal mper hour the hydrogen consumption ratio, to the expressed in mper hour under standard conditions the processed raw materials consumption, from 50 Nm/mup to 1000 Nm/mfor at least a portion of the sulfur compounds conversion into HS; b) stage of the formed HS removal, present in the withdrawn from stage a) stream, by the gasoline and hydrogen mixture cooling, hydrogen separation, enriched with hydrogen sulfide, from the liquid gasoline and gasoline stripping by the hydrogen stream introduction to remove the dissolved in gasoline hydrogen sulfide residual traces; c) withdrawn from stage b) HS depleted stream reacting in reactor with the catalyst comprising at least one sulfide of at least one transition metal, selected from the group VIB metal, group VIII metal and copper, separately or in the deposited on porous support mixture, in order to carry out the mercaptans with benzene olefins reaction with the thioether-type sulfur compounds formation, wherein the c) stage is carried out at a temperature from 30 °C to 250 °C, liquid volume velocity from 0.5 to 10 h, pressure of 0.4 to 5 MPa and the H/raw materials ratio from 0 to 10 Nmof hydrogen per mof raw materials with the gasoline production at the stage c) output, with fewer mercaptans amount than their amount in the taken from stage b) stream.EFFECT: process allows to achieve a very small amount of mercaptans in the final desulfurized gasoline under much less stringent operating conditions.18 cl, 4 dwg, 3 ex, 3 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 665 701 C2 (51) МПК C10G 65/06 (2006.01) C10G 45/08 ( ...

Method for preparing fuel oil from tar

本发明涉及用于焦油制燃料油的方法，主要解决现有技术中的脱硫率、脱氮率和燃油产率低的问题。本发明通过采用用于焦油制燃料油的方法，焦油和氢气为原料，在催化剂存在下进行反应制取燃料油，所述催化剂包括活性组分、助剂和载体；所述活性组分选自Ni，Mo和W中的任意一种，助剂包括Zn的技术方案取得了较好的效果，可用于煤焦油和/或乙烯焦油的加氢制燃料油中。

Adsorption desulfurization method for catalytically cracked gasoline

本发明涉及一种催化裂化汽油的吸附脱硫方法，采用固定床反应器，汽油与吸附脱硫催化剂接触，以重量百分比计，催化剂包括：25.0‑50.0wt％的氧化锌，0.5‑25.0wt％的氧化镍，2.0‑55.0wt％ZSM‑5分子筛，20.0‑50.0wt％的大孔氧化铝，1.0‑25.0wt％的铈锆固溶体；反应工艺条件为：反应温度280‑400℃，反应压力0.4‑2.5MPa，体积空速3‑8h ‑1 ，氢油体积比1‑50。催化剂穿透硫容高，辛烷值损失小，再生及还原稳定性好。

The preparation method of Mo-SBA-15 molecular sieve and hydrogenation catalyst

本发明涉及一种Mo‑SBA‑15分子筛的制备方法，合成步骤为将强酸体系中完成自组装但尚未进行水热处理的介孔材料SBA‑15，加入到含ⅥB族金属前驱体的溶液中，调节反应体系pH值在0～2之间，然后对其进行高温水热晶化处理，所得样品即为含ⅥB金属的SBA‑15分子筛。所得Mo‑SBA‑15分子筛具有高负载量、高分散度、高度有序介孔优点。以Mo‑SBA‑15分子筛为载体，仅需一步浸渍Ⅷ族金属过程即可制得具有大比表面积、优异的活性金属分散度、较高酸性的具有优异加氢脱硫性能的催化剂。

OIL OIL AND METHOD FOR PRODUCING OIL OIL

1. Способ получения нефтяного масла, включающий стадии фракционирования синтетической нефти, полученной синтезом Фишера Тропша, таким образом, что полученная промежуточная фракция, обладающая содержанием фракции с точкой кипения от 150 до 360°С, не менее 90 мас.%, и содержанием фракции с точкой кипения не менее 350°С не более 5 мас.%, и парафинового компонента, который является более тяжелым, чем промежуточная фракция, и приведения во взаимодействие каждого из указанных промежуточной фракции и парафинового компонента с катализатором гидрообработки в присутствии водорода, их смешивания, и фракционирования, так чтобы получить нефтяное масло, обладающее содержанием фракции с точкой кипения от 150 до 360°С не менее 86 мас.% и содержанием фракции с точкой кипения не менее 350°С не менее 5 мас.%. ! 2. Способ получения нефтяного масла по п.1, в котором указанная промежуточная фракция подвергается гидрообработке таким образом, что содержание углеводородов с точкой кипения не более 150°С в указанной промежуточной фракции на 3-9% больше после взаимодействия с указанным катализатором гидрообработки, чем перед взаимодействием. ! 3. Способ получения нефтяного масла по п.1 или 2, где указанный парафиновый компонент подвергают гидрообработке таким образом, что содержание фракции с точкой кипения не более 360°С в указанном парафиновом компоненте после взаимодействия с указанным катализатором гидрообработки составляет от 45 до 85 мас.%. ! 4. Способ получения нефтяного масла по по п.1 или 2, в котором каждый из указанных катализаторов гидрообработки приводят в контакт с указанной промежуточной фракцией, и указанный катализатор гидрообработки прив� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2008 140 146 (13) A (51) МПК C10G 65/14 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21), (22) Заявка: 2008140146/04, 14.02.2007 (71) Заявитель(и): НИППОН ОЙЛ КОРПОРЕЙШН (JP) (30) Конвенционный приоритет: 10.03.2006 JP 2006-066465 (87 ...

METHOD FOR PRODUCING GASOLINE WITH A SMALL QUANTITY OF SULFUR AND MERCAPTANES

1. Способ обработки бензина, содержащего соединения серы и олефины, причем способ включает по меньшей мере следующие этапы:a) взаимодействие, в по меньшей мере одном реакторе, бензина, водорода и катализатора гидродесульфирования при температуре от 200 до 400°C, давлении от 0,5 до 5 МПа, объемной скорости от 0,5 до 20 чи отношении расхода водорода, выраженного в нормальных мв час, к расходу обрабатываемого сырья, выраженному в мв час в стандартных условиях, от 50 Нм/мдо 1000 Нм/мдля превращения по меньшей мере части соединений серы в HS;b) этап удаления образованного HS, присутствующего в потоке, отбираемом с этапа a);c) взаимодействие в реакторе обедненного потока HS, отбираемого с этапа b), с катализатором, содержащим по меньшей мере один сульфид по меньшей мере одного переходного металла или свинца, осажденного на пористую подложку, причем этап c) осуществляют при температуре от 30°C до 250°C, объемной скорости жидкости от 0,5 до 10 ч, давлении от 0,4 до 5 МПа и отношении H/сырье от 0 до 25 Нмводорода на мсырья с получением на выходе этапа c) бензина, с меньшим количеством меркаптанов по сравнению с их количеством в потоке, отбираемом с этапа b).2. Способ по п. 1, в котором переходный металл катализатора на этапе c) выбран из металла группы VIB, металла группы VIII и меди, по отдельности или в смеси.3. Способ по п. 2, в котором катализатор на этапе c) включает:- подложку, состоящую из оксида алюминия гамма или дельта с удельной поверхностью от 70 м/г до 350 м/г;- массовое содержание оксида металла группы VIB от 1% до 30 масс.% от общей массы катализатора;- массовое содержание оксида металла группы VIII от 1% до 30 масс.% от общей массы катализатора;- степень сульфирования метал� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C10G 45/00 (13) 2014 124 384 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2014124384/04, 16.06.2014 (71) Заявитель(и): ИФП ЭНЕРЖИ НУВЕЛЛЬ (FR) Приоритет(ы): (30) Конвенционный ...

Production of diesel and base stocks from crude oil

Coal tar hydro-denitrificatiocatalyst catalyst and preparation method thereof

本发明公开了一种煤焦油加氢脱氮催化剂及其制备方法。该煤焦油加氢脱氮催化剂包括活性成分、助剂和载体，所述活性组分包括如下重量份数的组分：三硫化钨13‑15份、氧化镍5‑8份和三硫化钼3‑4份；所述助剂包括如下重量份数的组分：以单质计算，磷1‑2份、氟1‑4份；所述载体包括如下重量份数的组分：以载体干基计算，氧化铝45‑55份、Hβ分子筛5‑10份、二氧化钛10‑15份。本发明的有益效果为：该催化剂对于煤焦油加氢脱氮具有优异的活性。

Preparation method of hydrotreating catalyst carrier

本发明公开了一种加氢处理催化剂载体的制备方法。该方法包括：（i）以无定形硅铝干胶为原料，采用P123三嵌段共聚物为模板剂制备Al‑SBA‑15分子筛；（ii）将步骤（i）制备的Al‑SBA‑15介孔分子筛和氧化铝混捏成型，得到载体前驱体；（iii）用含有改性硅油的浸渍液浸渍步骤（ii）所得载体前驱体，然后经干燥、焙烧后得到所述加氢处理催化剂载体。采用本发明加氢处理催化剂载体制备的加氢处理催化剂适用于重质馏分油加氢处理工艺中，具有良好的活性。

METHODS FOR PRODUCING OLEFIN PRODUCT

1. Способ получения олефинового продукта, включающий стадии:(a) реагирование оксигенатного сырья, содержащего оксигенат, в реакционной зоне оксигенатов в присутствии катализатора, содержащего молекулярное сито, при температуре в диапазоне от 350°C до 1000°C, с образованием выходящего потока реакции, содержащего по меньшей мере оксигенат, олефин, воду и кислотные побочные продукты;(b) необязательного охлаждения выходящего потока реакции с помощью косвенного теплообмена до температуры, превышающей температуру точки росы выходящего потока реакции;(c) дальнейшего быстрого охлаждения выходящего потока реакции до температуры ниже температуры точки росы выходящего потока реакции с помощью прямого инжектирования водосодержащей жидкости в выходящий поток реакции, с образованием первого закаленного выходящего потока; и(d) разделения первого закаленного выходящего потока на первый жидкий закаленный выходящий поток и первый газообразный закаленный выходящий поток, содержащий олефиновый продукт, при этом на стадии (с) водосодержащую жидкость инжектируют с помощью закалочного фитинга.2. Способ по п. 1, в котором на стадии (b) выходящий поток реакции охлаждают до температуры в диапазоне от 140°C до 370°C.3. Способ по п. 1 или 2, в котором на стадии (с) водосодержащую жидкость впрыскивают непосредственно в трубопровод, транспортирующий выходящий поток реакции.4. Способ по п. 1 или 2, в котором закалочный фитинг содержит распылительную форсунку.5. Способ по п. 1 или 2, в котором на стадии (с) выходящий поток реакции охлаждают таким образом, что первый закаленный выходящий поток имеет температуру в диапазоне от 30°C до 100°C.6. Способ по п. 1 или 2, в котором на стадии (с) выходящий поток реакции РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C07C 1/20 (13) 2015 120 584 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2015120584, 29.10.2013 (71) Заявитель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) Приоритет(ы): (30) ...

Method for producing winter and arctic diesel fuels from straight-run diesel fractions with a sulfur content of up to 5000 mg/kg and nitrogen up to 200 mg/kg

FIELD: oil refining industry. SUBSTANCE: invention relates to the field of catalysis in oil refining. A method for producing winter and arctic diesel fuels from straight-run diesel fractions with a sulfur content of up to 5000 mg/kg and nitrogen up to 200 mg/kg is described, which provides for sequential processing of raw materials using a catalytic system, characterized by the fact that raw materials are processed by combining hydrotreating and isodeparaffinization processes without intermediate separation of products using a catalytic system that includes the following catalytic layers of catalysts in the direction of movement of raw materials: a catalyst for preliminary hydrotreating; hydrotreating catalyst containing, wt. %: nickel oxide 4.0-10.0, molybdenum oxide 15.0-25.0, phosphorus oxide 0.5-5.0, silicon oxide 1.0-10.0, Al 2 O 3 being the rest; isodeparaffinization catalyst containing, wt. %: platinum 0.4-0.8, carrier being the rest, while the carrier contains: zeolite EU-2 30-80, γ-Al 2 O 3 20-70; hydrofinishing catalyst. EFFECT: increase in the yield of the target product without deterioration of its quality. 3 cl, 6 tbl, 5 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 758 847 C1 (51) МПК C10L 1/08 (2006.01) C10G 11/00 (2006.01) C10G 45/64 (2006.01) C10G 45/12 (2006.01) C10G 65/00 (2006.01) B01J 29/74 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10L 1/08 (2021.05); C10G 11/00 (2021.05); C10G 45/64 (2021.05); C10G 45/12 (2021.05); C10G 65/00 (2021.05); B01J 29/74 (2021.05) (21)(22) Заявка: 2021107748, 24.03.2021 24.03.2021 Дата регистрации: 02.11.2021 (45) Опубликовано: 02.11.2021 Бюл. № 31 2 7 5 8 8 4 7 R U (56) Список документов, цитированных в отчете о поиске: WO 2013085533 A1, 13.06.2013. Герасимов Денис Николаевич Изодепарафинизация нефтяного сырья на платиновых цеолитсодержащих катализаторах. Автореферат диссертации на соискание ученой степени кандидата химических наук. Москва, 2014. RU ...

Extremely low acidity USY and homogeneous, amorphous silica-alumina hydrocracking catalyst and process

公开一种催化剂组合物，包含：少量的α值小于约5、优选小于约3而且通过FT－IR测量的布朗斯台德酸度为约1至约20、优选约1－10μmol/g的低酸度、高度脱铝的超稳定Y沸石；SB比为约0.7至约1.3的均匀非晶形氧化硅－氧化铝裂化组分，其中结晶氧化铝相的量不大于约10％、优选不大于5％；和催化量的选自第VI族金属、第VIII族金属及其混合物的氢化组分。本发明提供一种烃油转化方法，包括使烃油与所述催化剂在适合的烃转化条件下接触。此类过程包括但不限于单级加氢裂化、两级加氢裂化、串流加氢裂化、缓和加氢裂化、生产润滑油的加氢裂化、加氢处理、润滑油加氢精制、加氢脱硫、加氢脱氮、催化脱蜡和催化裂化。

Preparation method of hydrotreating catalyst, hydrotreating catalyst and application

本发明公开了一种加氢处理催化剂的制备方法及加氢处理催化剂和应用。本发明的加氢处理催化剂的制备方法，包括：（i）制备Beta/Al‑SBA‑15复合分子筛；（ii）将步骤（i）所得Beta/Al‑SBA‑15复合分子筛与氧化铝干胶粉经混捏、成型、干燥和焙烧，得到加氢处理催化剂载体；（iii）将含有有机助剂和活性金属组分的浸渍液浸渍步骤（ii）所得加氢处理催化剂载体，然后经两步干燥得到加氢处理催化剂。采用本发明方法制备的加氢处理催化剂能够深度脱除煤焦油中含氮化合物，加氢性能好，满足后续工序生产的质量要求，充分发挥裂化催化剂的使用性能。

Preparation method of hydrotreating catalyst, hydrotreating catalyst and application

本发明公开了一种加氢处理催化剂的制备方法及加氢处理催化剂和应用。本发明的加氢处理催化剂的制备方法，包括：（I）制备Al‑SBA‑15分子筛；（II）将步骤（I）制备的Al‑SBA‑15分子筛和氧化铝混捏成型，得到载体前驱体；（III）用含有纳米二氧化硅分散液浸渍步骤（II）所得载体前驱体，然后经干燥得到所述加氢处理催化剂载体；（IV）用含有活性金属组分的浸渍液浸渍步骤（III）所得载体，然后经干燥、焙烧得到加氢处理催化剂。采用本发明方法制备的加氢处理催化剂能够深度脱除煤焦油中含硫、含氮化合物，加氢性能好，满足后续工序生产的质量要求，充分发挥裂化催化剂的使用性能。

Gasoline hydrofining catalyst and preparation method thereof

本发明公开了一种汽油加氢精制催化剂及其制备方法。该催化剂包括氧化铝、改性TS‑1分子筛和活性金属组分，其中活性金属组分为氧化钼和氧化钴。该加氢精制催化剂适用于FCC汽油加氢精制，具有高活性、高选择性和使用寿命长的特点，不但具有较高的液体产品收率，而且还可以使产品能够既能够满足汽油国六标准中硫含量的要求、烯烃含量要求、以及芳烃含量要求，又能够减小辛烷值的损失。

Method of converting paraffin-containing hydrocarbon crude

FIELD: petrochemical industry. SUBSTANCE: invention aims at reducing paraffin in paraffin-containing hydrocarbon crude to produce middle-run products including low freezing-point jetliner fuel and/or diesel fuel as well as densified oil with low flow and cloud points. Initial material is brought into contact with hydrocracking catalyst in hydrocracking zone in presence of hydrogen at elevated temperature and pressure, where catalyst contains filling agent, at least one hydrogenated metal component selected from the group including VIB and VIII group metals, and large-pore size zeolite (Y-type zeolite). Hydrocracking product stream enters hydrodewaxing zone, where, at elevated temperature and pressure and in presence of hydrogen, product is brought into contact with dewaxing catalyst containing crystalline molecular sieve with transitory-size pores selected from the group including borosilicates, ferrosilicates, aluminosilicates, and silicoaluminophosphates. EFFECT: improved working characteristics of products. 6 cl, 4 tbl, 2 ex рзэЭэзстс ПЧ ГЭ РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) (51) МПК ВИ "” 2 128 681 ' 13) Сл С 10 С 65/12 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 96108801/04, 07.10.1994 (30) Приоритет: 08.10.1993 ЕР 93202853.3 (46) Дата публикации: 10.04.1999 (56) Ссылки: Ц$ 4743354 А, 10.05.88. ЗЦ 757588 АЛ, 23.08.80. 0$ 4347121 А, 31.08.82. ЕР 0042238 АЛ, 23.12.81. ЕР 0263228 А2, 13.04.88. ЕР 0233169 АД, 19.08.87. (85) Дата перевода заявки РСТ на национальную фазу: 08.05.96 (86) Заявка РСТ: ЕР 94/03323 (87) Публикация РСТ: М/О 95/10578 (20.04.95) (98) Адрес для переписки: 103735, Москва, ул.Ильинка, 5/2, Союзпатент (71) Заявитель: Акцо Нобель Н.В. (М), Файна Резеч С.А. (ВЕ) (72) Изобретатель: Йоханнес Вильхельмус Мария Соннеманс (МЕ), Франсискус Мария Ноэй (МГ), Жак Франсуа Жан Гротьянс (ВЕ) (73) Патентообладатель: Акцо Нобель Н.В. (М), Файна Резеч С.А. (ВЕ) (54) СПОСОБ ПРЕВРАЩЕНИЯ ПАРАФИНСОДЕРЖАЩЕГО ...

Method for processing low-grade heavy oil

本发明提供了一种加工劣质重油的方法，该方法包括：将劣质重油进行选择性溶剂脱沥青，得到脱沥青油；将脱沥青油或其他重油原料与氢气混合进行加氢处理，得到加氢重油；将加氢重油作为催化裂化的原料进行催化裂化转化，催化裂化过程中得到液体轻质产品与重油油浆；其中，所述液体轻质产品包括汽油、柴油和/或液化气；将催化裂化得到的重油油浆掺入到选择性溶剂脱沥青的劣质重油原料中。本发明的方法是一种将高杂质含量重油加工为车用汽柴油的组合加工方法，适于加工硫氮含量高、金属含量高、沥青质含量或残炭值高的劣质重馏分油或渣油等高杂质含量重油。本发明的加工技术具有汽柴油及液化气组分收率高、产品质量好、环境污染物排放少等特点。

High-stability catalyst of heavy hydrocarbon wet desulfurisation and methods of its production

FIELD: process engineering. SUBSTANCE: invention relates to catalyst of heavy hydrocarbon desulfurisation, method of its production and method of desulfurisation of heavy hydrocarbons. Proposed catalyst includes calcined mix produced by calcinating formed particle made by grinding the mix containing molybdenum trioxide, nickel compound and inorganic oxide material. Proposed method of producing said catalyst comprises grinding inorganic oxide material, molybdenum trioxide and nickel compound to produce mix to be formed in particle and calcined to obtain aforesaid mix. Method of desulfurisation of heavy hydrocarbon initial stock comprises interaction of the latter with aforesaid catalyst. EFFECT: purified product with higher stability. 11 cl, 10 tbl, 6 ex, 2 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 443 472 (13) C2 (51) МПК B01J B01J B01J C10G 23/88 (2006.01) 37/04 (2006.01) 37/08 (2006.01) 45/08 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2009107513/04, 01.08.2007 (24) Дата начала отсчета срока действия патента: 01.08.2007 (73) Патентообладатель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) R U Приоритет(ы): (30) Конвенционный приоритет: 03.08.2006 US 60/821,341 (72) Автор(ы): БХАН Опиндер Кишан (US) (43) Дата публикации заявки: 10.09.2010 Бюл. № 25 2 4 4 3 4 7 2 (45) Опубликовано: 27.02.2012 Бюл. № 6 (56) Список документов, цитированных в отчете о поиске: GB 2118062 А, 26.10.1983. GB 2118063 A, 26.10.1983. GB 2055602 A, 11.03.1981. RU 98105317 А, 27.01.2000. RU 2197323 C1, 27.01.2003. 2 4 4 3 4 7 2 R U (86) Заявка PCT: US 2007/074961 (01.08.2007) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 03.03.2009 (87) Публикация заявки РСТ: WO 2008/016969 (07.02.2008) Адрес для переписки: 129090, Москва, ул.Б.Спасская, 25, стр.3, ООО "Юридическая фирма Городисский и Партнеры", пат.пов. Е.Е.Назиной (54) ВЫСОКОСТАБИЛЬНЫЙ КАТАЛИЗАТОР ГИДРООБЕССЕРИВАНИЯ ТЯЖЕЛЫХ УГЛЕВОДОРОДОВ И СПОСОБЫ ...

Gasoline hydrofining catalyst and preparation method thereof

本发明公开了一种汽油加氢精制催化剂，包括氧化铝、改性KIT‑6分子筛和活性金属组分，其中活性金属组分为氧化钼和氧化钴。本发明还公开了所述的汽油加氢精制催化剂的制备方法以及一种FCC汽油加氢精制的方法。使用本发明的催化剂对FCC汽油原料进行加氢精制，不但具有较高的液体产品收率，还可以使产品既能够满足汽油国六标准中硫含量的要求、烯烃含量要求、以及芳烃含量要求，又能够减小辛烷值的损失。

Catalyst for hydrogenation refining of cracked tar

本发明涉及裂解焦油加氢精制的催化剂，主要解决现有技术中的脱硫率、脱氮率和燃油产率低的问题。本发明通过采用裂解焦油加氢精制的催化剂，所述催化剂包括活性组分、助剂和载体；所述活性组分包括选自Co，Mo和W中的任意一种，助剂包括Sb的技术方案取得了较好的效果，可用于煤焦油和/或乙烯焦油的加氢制燃料油中。

Process for preparing basestocks having high vi

一种制备高VI润滑油基础料的方法，包括加氢处理、加氢脱蜡和可选择地加氢精制。加氢处理步骤的条件使得转化成343℃以下的量基础料小于5wt％并且较进料VI的VI增加值小于4。加氢脱蜡使用低α催化剂并且加氢精制采用基于M41S类的催化剂实现。

Catalytic composition for refining hydrocarbon mixtures, method for preparation thereof (options), and method of hydrofining of hydrocarbon mixtures

FIELD: petroleum processing catalysts. SUBSTANCE: invention related to hydrofining of hydrocarbon mixtures with boiling range 35 to 250 о С and containing no sulfur impurities provides catalytic composition containing β-zeolite, group VIII metal, group VI metal, and possibly one or more oxides as carrier. Catalyst is prepared either by impregnation of β-zeolite, simultaneously or consecutively, with groups VIII and VI metal salt solutions, or by mixing, or by using sol-gel technology. EFFECT: increased isomerization activity of catalytic system at high degree of hydrocarbon conversion performed in a single stage. 40 cl, 2 tbl, 19 ex ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß (19) RU (51) ÌÏÊ 7 (11) (13) 2 245 191 C2 B 01 J 29/06, 23/882, 23/883, 37/02, 37/04, C 10 G 45/08, 45/60 ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2000105594/04, 10.03.2000 (72) Àâòîð(û): ÄÇÀÍÈÁÅËËÈ Ëàóðà (IT), ÔÅÐÐÀÐÈ Ìàðêî (IT), ÀÐÐÈÃÎÍÈ Âèðäæèíèî (IT) (24) Äàòà íà÷àëà äåéñòâè ïàòåíòà: 10.03.2000 (30) Ïðèîðèòåò: 12.03.1999 IT MI99A000504 (45) Îïóáëèêîâàíî: 27.01.2005 Áþë. ¹ 3 (57) Ðåôåðàò: Íàñòî ùåå èçîáðåòåíèå îòíîñèòñ ê êàòàëèòè÷åñêîé êîìïîçèöèè, ñïîñîáàì åãî ïðèãîòîâëåíè è ñïîñîáó ãèäðîî÷èñòêè óãëåðîäíûõ ñìåñåé, èìåþùèõ äèàïàçîí êèïåíè â èíòåðâàëå îò 35 äî 250°Ñ, ñîäåðæàùèõ ïðèìåñè ñåðû. Îïèñàíà êàòàëèòè÷åñêà êîìïîçèöè , ñîäåðæàùà áåòà-öåîëèò, ìåòàëë VIII ãðóïïû, ìåòàëë VI â ãðóïïû, âîçìîæíî, îäèí èëè áîëåå îêñèäîâ â êà÷åñòâå íîñèòåë . Îïèñàíû ñïîñîáû åå ïðèãîòîâëåíè (âàðèàíòû) ïóòåì ïðîïèòêè áåòà-öåîëèòà îäíîâðåìåííî èëè ïîñëåäîâàòåëüíî ðàñòâîðàìè ñîëåé ìåòàëëîâ VIII è VI â ãðóïï, ëèáî ñìåøåíèåì, ëèáî ïîñðåäñòâàì çîëü-ãåëåâîé òåõíîëîãèè. Îïèñàí òàêæå ñïîñîá ãèäðîî÷èñòêè óãëåðîäíûõ ñìåñåé ñ èñïîëüçîâàíèåì âûøåóêàçàííîé êàòàëèòè÷åñêîé êîìïîçèöèè. Òåõíè÷åñêèé ýôôåêò — ïîâûøåííà èçîìåðèçóþùà àêòèâíîñòü êàòàëèòè÷åñêîé ñèñòåìû, âûñîêà ñòåïåíü êîíâåðñèè ñìåñè óãëåðîäîâ, îñóùåñòâëåíèå ïðîöåññà â îäíó ñòàäèþ. 9 í. è 31 ç.ï. ...

Catalyst and process for the hydrodenitrogenation and hydrocracking of high-nitrogen feeds

There is disclosed a catalyst, which catalyst comprises a hydrogenation component comprising chromium, molybdenum, and at least one metal of Group VIII, a crystalline molecular sieve zeolite, and a porous refractory inorganic oxide. Suitable molecular sieve zeolites are those having pore diameters of at least 5 Å (0.5 nm) and containing exchangeable cations, for example, faujasite-type crystalline aluminosilicates, mordenite-type crystalline aluminosilicates, ZSM-type crystalline aluminosilicates, and AMS-type crystalline metallosilicates. There is also disclosed a process, which process comprises contacting a hydrocarbon stream containing a substantial amount of nitrogen under hydrotreating conditions and in the presence of hydrogen with the aforesaid catalyst.

Process for preparing basestocks having high vi

A process for preparing high VI lubricating oil basestocks comprising hydrotreating, hydrodewaxing and optionally hydrofinishing. The hydrotreating step is under conditions such that the amount of conversion to 343~C minus is less than 5wt% of the feedstock and the VI increase is less than 4 VI over the feedstock. Hydrodewaxing uses a low alpha catalyst and hydrofinishing is accomplished with a catalyst based on the M41S family.

PROCESS FOR THE SOFT HYDROCRACKING OF OIL CUTTINGS WITH A CATALYST CONTAINING AT LEAST TWO DESALUMINATED ZEOLITHS

Preparation method of dipping solution and dipping solution prepared by method

本发明涉及一种浸渍溶液的制备方法及由该方法制得的浸渍溶液，所述方法包括：(1)配制含有至少一种含第VIII族金属的化合物和至少一种含第一种第VIB金属的化合物的第一溶液；(2)将第一溶液在大于0.1MPa至小于等于10MPa的压力下进行活化处理，处理温度为65℃～200℃，时间为0.5‑36小时；(3)待活化处理后的第一溶液温度降至室温～50℃后，向其中引入至少一种含第二种第VIB金属的化合物，得到所述浸渍溶液。采用本发明提供的浸渍溶液浸渍载体制备的加氢催化剂，其加氢精制或加氢处理性能明显提高。

METHOD FOR HYDROPROCESSING A GAS FUEL LOAD, HYDROTREATING REACTOR FOR CARRYING OUT SAID METHOD, AND CORRESPONDING HYDROREFINING UNIT

Catalytic hydrotreatment of gas oil feedstock and biological origin of vegetable oil- and animal fat feedstock in a unit, comprises injecting oil feedstock in first reactor, and injecting biological feedstock in first and second reactors

The process for catalytic hydrotreatment of gas oil feedstock and biological origin of vegetable oil- and animal fat feedstock (less than 15 wt.%) in a unit with fixed bed, comprises injecting the oil feedstock in a first reactor, injecting a part of the biological feedstock in the first reactor and other part in a second reactor, injecting a liquid effluent withdrawn from the first reactor in the second reactor, and effecting a supplementary treatment of carbon monoxide present in the gas recycled from the hydrotreatment of the total feedstock. The process for catalytic hydrotreatment of gas oil feedstock and biological origin of vegetable oil- and animal fat feedstock (less than 15 wt.%) in a unit with fixed bed, comprises injecting the oil feedstock in a first reactor, injecting a part of the biological feedstock in the first reactor and other part in a second reactor, injecting a liquid effluent withdrawn from the first reactor in the second reactor, effecting a supplementary treatment of carbon monoxide present in the gas recycled from the hydrotreatment of the total feedstock, and controlling the exothermicity of the biological feedstock hydrotreatment using a thermal regulation system. The gas oil feedstock is a gas fraction originating from distillation of crude oil and/or synthetic crude obtained from the treatment of bituminous schists, other heavy crude oils or effluent of Fischer Tropsch process, and originating from catalytic and/or thermal cracking (fluid catalytic cracking, coking, visbreaking). The catalytic injection zone of the biological feedstock comprises a first catalytic bed trap with metals. A quantity of hydrogen (120-450 Normoliters per liters of gas oil feedstock, and 200-1000 Normoliters per liters of biological feedstock) is introduced in the first and second catalytic zone respectively. The gas oil feedstock and biological feedstock are treated in the first and second catalytic zone at a temperature of 340-400[deg] C and 280-350[deg] C ...

A kind of carbon containing catalyst for hydro-upgrading and preparation method thereof

本发明公开一种加氢改质催化剂及其制备方法和应用，所述加氢改质催化剂以催化剂的重量为基准，催化剂载体的含量为55.0wt％~94.5wt％，第VIB族金属氧化物含量为5.0wt％~30.0wt％，第VIII族金属氧化物含量为0.5wt％~15.0 wt％，所述催化剂载体以重量为基准分子筛的含量为3%~35%，氧化铝的含量为55%~95%，二氧化硅计的含量为0.2％～10.0％，碳的含量为0.4％～10％，助剂氧化物含量为0.2%~20.0%。该催化剂用于柴油加氢改质过程中，具有深度加氢脱硫活性，并能在保持柴油收率较高的情况下改善十六烷值等综合性能。

HYDRORAFFINAGE CATALYST CONTAINING RUTHENIUM SULFIDE, ITS SYNTHESIS AND HYDRORAFFINAGE PROCESS USING THE SAME.

PROCESS FOR IMPROVING THE FLOW POINT OF PARAFFINIC LOADS WITH A ZEOLITHE IM-5 BASED CATALYST

Lubricating oils with improved colour and - stability

Lubricating oils with improved props. are obtd. by contacting, under hydrogenation condits., with a catalyst comprising a group VIII metal deposited on a support consisting of a cation-free mordenitic zeolite. Spec., the catalyst consists of 0.1-5% wt. Pt or Pd or palladium, or 1-10% wt. Fe deposited on a mordenite contg. hydrogen ions. The lubricating oil is first treated with a solvent to remove paraffin, and may also be treated with an acid. It is desulphurised to give an oil with a predetermined sulphur content. The lubricanting oil is pref. a naphthenic oil. The cation-free zeolite is obtained by treating the zeolite with an acid.

A method of improving oil product deep hydrodesulfurizationof

本发明涉及一种油品深度加氢脱硫方法，在固定床反应体系中进行DBT深度加氢脱硫，采用设计特定的多重乳液体系，制备空心球形SBA‑15载体材料，并通过铝修饰改善SBA‑15水热稳定性并提高其酸性位数量，然后采用等体积分布浸渍法将金属活性组分负载到载体上，通过采用制备得到的空心球状NiMo/SBA‑15‑SP催化剂，不仅具有适宜的MoS 2 分散度和B、L酸性位数量，还具有优异的DBT反应分子扩散性能，能够提高其总体反应速率，对二苯并噻吩(DBT)加氢脱硫反应活性进行评价，显示出优异的DBT脱硫转化频率TOF和速率常数，具备良好的应用前景。

Production of low color middle distillate fuels

In a process for producing a low color diesel and/or kerosene fuel, a middle distillate feed can be supplied to a reactor having at least one first catalyst bed containing a first desulfurization and/or isomerization catalyst and at least one second catalyst bed containing a decolorization catalyst downstream from the first catalyst bed(s). The feed can be reacted with the hydrogen in the presence of the first catalyst at a temperature from about 290°C to about 430°C to produce a first liquid effluent, which can be cooled by about 10°C to about 40°C with a quench medium and cascaded to the at least one second catalyst bed. The cooled first liquid effluent can then be reacted with hydrogen in the presence of the decolorization catalyst at a temperature from about 280°C to about 415°C to produce a second effluent having an ASTM color less than 2.5.

The desulfurizing method by adsorption of catalytically cracked gasoline

本发明涉及一种催化裂化汽油的吸附脱硫方法，采用固定床反应器，汽油与吸附脱硫催化剂接触，以重量百分比计，催化剂包括：25.0‑50.0wt％的氧化锌，0.5‑25.0wt％的氧化镍，2.0‑55.0wt％ZSM‑5分子筛，20.0‑50.0wt％的大孔氧化铝，1.0‑25.0wt％的铈锆固溶体；反应工艺条件为：反应温度280‑400℃，反应压力0.4‑2.5MPa，体积空速3‑8h ‑1 ，氢油体积比1‑50。催化剂穿透硫容高，辛烷值损失小，再生及还原稳定性好。

Process for producing a gasoline with a low sulphur and mercaptans content

본 발명은 황-함유 화합물 및 올레핀을 포함하는 가솔린의 처리 방법을 제공하며, 이 방법은 적어도 이하의 단계를 포함한다: a) 황이 감소한 용출액을 생성하기 위하여, 적어도 하나의 수소화탈황 촉매 상에서 수소와 함께 혼합된 가솔린을 통과시키는 것을 포함하는 가솔린의 수소화탈황 단계; b) 단계 a)에서 생성된 H 2 S 뿐만 아니라 과량으로 도입된 수소로부터 부분적으로 탈황된 가솔린을 분리하는 단계; c) 올레핀과의 부가 반응을 통해 티오에테르로 잔류 메르캅탄을 변환시키는, 단계 b)로부터 얻어진 탈황 가솔린을 스위트닝하는 촉매 단계.

THE UNITED METHOD OF HYDROCRACKING AND DEPARAFFINING OF HYDROCARBONS

1. Способ получения лигроинового топлива, дизельного топлива и базового смазочного масла, включающий:приведение в контакт гидроочищенного сырья и водородсодержащего газа с катализатором гидрокрекинга при условиях, эффективных для гидрокрекинга, для получения обработанного гидрокрекингом выходящего потока,направление нисходящим потоком всего обработанного гидрокрекингом выходящего потока, без разделения, в стадию каталитической депарафинизации, идепарафинизацию всего обработанного гидрокрекингом выходящего потока при условиях, эффективных для каталитической депарафинизации, в котором объединенное общее содержание серы в жидкой и газообразной формах, подаваемой в стадию депарафинизации, составляет более 1000 мас.ч./млн серы по отношению к гидроочищенному сырью,где катализатор гидрокрекинга включает катализатор на основе цеолита Y, игде катализатор депарафинизации включает по меньшей мере один недеалюминированный цеолит с одноразмерными порами, образованными десятичленными кольцами и по меньшей мере один металл группы VIII.2. Способ по п.1, в котором катализатор депарафинизации дополнительно включает по меньшей мере одно огнеупорное связующее на основе оксида металла с низкой площадью поверхности.3. Способ по п.1, в котором до стадии приведения в контакт выходящий из стадии гидроочистки поток подают по меньшей мере в один сепаратор высокого давления для отделения газообразной фракции гидроочищеного выходящего потока от жидкой фракции гидроочищенного выходящего потока.4. Способ по п.2, в котором до стадии приведения в контакт выходящий из стадии гидроочистки поток подают по меньшей мере в один сепар РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C10G 47/00 (13) 2011 129 062 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2011129062/04, 30.12.2009 (71) Заявитель(и): ЭкссонМобил Рисерч энд Энджиниринг Компани (US) Приоритет(ы): (30) Конвенционный приоритет: 31.12.2008 US 61/204,057; 23.12.2009 US 12/655,128 (85) ...

catalyst comprising a partially amorphous zeolite and hydrocarbon charge hydroconversion process.

Processes for the preparation of an olefinic product

本发明提供了用于制备烯属产物的方法，所述方法包括以下步骤：(a)在350‑1000℃的温度下，在含分子筛的催化剂存在下，在含氧化合物反应区中使包含含氧化合物的含氧化合物原料反应，以产生至少包含含氧化合物、烯烃、水和酸性副产物的反应流出物物流；(b)通过间接换热来冷却反应流出物物流至大于反应流出物物流的露点温度的温度；(c)通过将含水液体直接注入反应流出物物流来进一步快速冷却反应流出物物流至低于反应流出物物流的露点温度的温度，以形成第一急冷流出物物流；和(d)将第一急冷流出物物流分为第一液态急冷流出物物流和包含烯属产物的第一气态急冷流出物物流。

HYDROREFINING CATALYST CONTAINING RUTHENIUM SULFIDE, ITS SYNTHESIS AND HYDROREFINING PROCESS USING THE CATALYST.

Cette invention concerne un catalyseur d'hydroraffinage renfermant du sulfure de ruthénium sur zeolithe non-acide, particulièrement efficace pour les réactions d'hydrodésazotation.

Wax oil hydrogenation catalyst and preparation method thereof

一种蜡油加氢催化剂，包括载体和活性组分，活性组分负载于载体之上，以杂多酸为活性组分，Al 2 O 3 ‑TS‑1‑ZrO 2 ‑石墨烯复合氧化物为载体；所述催化剂比表面积为250～500m 2 /g，孔容0.5～0.8mL/g。该催化剂制备方法为将分子筛、氧化铝、氧化锆及石墨烯混合均匀后，加入硝酸溶液及适量水，经混捏、挤条、干燥、焙烧后制得本发明的催化剂载体。载体用含杂多酸的溶液浸渍，经干燥、焙烧后即得到本发明催化剂。该催化剂具备特定孔径、较大孔容，较高加氢脱硫、脱氮活性等特点，可作为蜡油加氢催化剂使用。

Preparation method of isomerization catalyst taking TON type structure molecular sieve as carrier

本发明公开了一种以TON型结构分子筛为载体的异构化催化剂的制备方法。催化剂制备的具体步骤如下：首先在100‑400℃下对具有TON型结构的分子筛原粉进行部分脱模处理；再将第VIII族贵金属活性组分负载于处理后的分子筛上；然后在氢气气氛中还原得到目标催化剂。通过控制分子筛载体中模板剂的脱除方式，实现了催化剂金属性质、酸性质和孔道性质的有效调控。与现有技术制得的催化剂相比，采用本发明方法制得的催化剂在正构烷烃异构化反应中表现出了高的反应活性和异构体收率。

Method for the hydro-processing of a gas oil feedstock, and corresponding hydro-refining unit

本发明涉及用于在固定床催化加氢处理装置中对柴油类石油原料和含有植物油和/或动物脂的生物原料进行催化加氢处理的方法，所述方法的特征在于，石油原料在生物原料上游被引入到所述反应器中。本发明还涉及用于实现所述方法的催化加氢处理装置以及相应的加氢精制装置。