КОМПОЗИЦИЯ КАТАЛИЗА, ПРЕДНАЗНАЧЕННАЯ ДЛЯ ПЕРЕРАБОТКИ ТЯЖЕЛОГО ИСХОДНОГО СЫРЬЯ

Изобретение относится к катализаторам крекинга тяжелого сырья. Описан способ получения модифицированного цеолитного катализатора, включающий формирование суспензии, содержащей от 15 до 55% масс. матричного компонента, выбираемого из группы, состоящей из глин, синтетической матрицы, отличной от столбчатой глины, и их смесей, и от 10 до 20% масс. золя или геля связующего, выбираемого из группы, состоящей из оксидов алюминия, кремния и их смесей, и от 0 до 15% масс. оксида металла группы IVB или VB, добавление сюда от 10 до 75% масс. смеси цеолитов, выбираемых из группы, состоящей из: (i) подвергнутого обработке щелочью селективного цеолита, обладающего структурой, у которой отношение диоксида кремния и оксида алюминия меньше 45, а определенная по методу БЭТ площадь удельной поверхности пор в диапазоне от мезопор до больших пор превышает 50 м2/г; (ii) олефинселективного цеолита, обладающего структурой, у которой отношение диоксида кремния и оксида алюминия меньше 70; (iii) бета-цеолита, обладающего ...

ПРИЕМЛЕМЫЙ ДЛЯ ПРИМЕНЕНИЯ ПРИ ГИДРОКОНВЕРСИИ КАТАЛИЗАТОР, СОДЕРЖАЩИЙ ПО МЕНЬШЕЙ МЕРЕ ОДИН ЦЕОЛИТ И МЕТАЛЛЫ ИЗ ГРУПП VIII И VIB, И ПОЛУЧЕНИЕ КАТАЛИЗАТОРА

Изобретение относится к катализатору гидроконверсии, содержащему цеолит, к способу его получения и к способу гидроконверсии углеводородных смесей, при котором применяют этот катализатор. Катализатор содержит носитель, включающий по меньшей мере одно связующее и цеолит, выбранный из FAU и/или BEA, фосфор, по меньшей мере один диалкилсукцинат C1-C4, уксусную кислоту и функциональную группу с гидрирующей-дегидрирующей способностью, содержащую по меньшей мере Mo и Ni. В спектре комбинационного рассеяния этого катализатора присутствуют характеристические полосы по меньшей мере одного гетерополианиона Кеггина в области 990 см, основная характеристическая полоса уксусной кислоты в области 896 сми характеристические полосы указанного сукцината. Технический результат – расширение арсенала катализатора гидроконверсии. 3 н. и 18 з.п. ф-лы, 1 ил., 6 табл., 6 пр.

КОМПОЗИЦИЯ КАТАЛИЗАТОРА ГИДРОКРЕКИНГА

Изобретение относится к композициям катализатора гидрокрекинга, их получению и применению в процессе гидрокрекинга. Композиция катализатора без носителя для гидрокрекинга включает в себя один или несколько металлов группы VIb, один или несколько неблагородных металлов группы VIII, один или несколько цеолитов и, необязательно, тугоплавкий оксидный материал, получена осаждением металлов группы VIb, неблагородных металлов группы VIII, и, необязательно, тугоплавкого оксидного материала в присутствии цеолита. Способ получения вышеуказанной композиции катализатора, в котором одно или несколько соединений металлов группы VIb объединяют с одним или несколькими соединениями неблагородных металлов группы VIII, и с цеолитом, в присутствии протоносодержащей жидкости и щелочного соединения, и после осаждения извлекают композицию катализатора. Технический результат - получение каталитической композиции, обладающей очень высокой активностью при гидрировании моноароматических соединений, а также существенно ...

Модифицированное молекулярное сито типа Y и способ его получения, катализатор гидрокрекинга и способ его получения и способ гидрокрекинга нефтяного масла

Изобретение относится к области техники гидрокрекинга, и в нем описывают модифицированное молекулярное сито типа Y и способ его получения, катализатор гидрокрекинга и способ его получения и способ гидрокрекинга нефтяного масла. Модифицированное молекулярное сито типа Y содержит 0,5-2 мас.% Na2O по отношению к общему количеству модифицированного молекулярного сита типа Y, причем отношение общего количества кислоты модифицированного молекулярного сита типа Y, измеренного с помощью пиридина и инфракрасной спектрометрии, и общего количества кислоты модифицированного молекулярного сита типа Y, измеренного с помощью н-бутилпиридина и инфракрасной спектрометрии, составляет 1-1,2, при этом общее количество кислоты модифицированного молекулярного сита типа Y, измеренное с помощью пиридина и инфракрасной спектрометрии, составляет 0,1-1,2 ммоль/г. Способ получения модифицированного молекулярного сита типа Y содержит следующие стадии: (1) предварительная обработка молекулярного сита NaY с получением ...

ПОКРЫТИЕ ДЛЯ ВОССТАНОВЛЕНИЯ ОКСИДОВ АЗОТА

... 1. Каталитическое покрытие для применения в качестве гидролитического катализатора (Г-катализатора) для восстановления оксидов азота, отличающееся тем, что в качестве соединения, адсорбирующего HNCO и оксиды азота, Г-катализатор содержит лантан и дополнительно содержит одно или несколько соединений, являющееся или являющихся щелочным и/или щелочно-земельным металлом, и/или иттрием, и/или гафнием, и/или празеодимом, и/или галлием, и/или цирконием.2. Каталитическое покрытие по п. 1, отличающееся тем, что Г-катализатор содержит каталитическое покрытие на основе диоксида титана, предпочтительно в форме анатаза, на основе SiO, на основе цеолита, предпочтительно ZSM-5 и/или в бета форме, и/или на основе двуокиси циркония.3. Каталитическое покрытие по п. 1 или 2, отличающееся тем, что Г-катализатор содержит восстановитель, являющийся мочевиной и/или восстановитель, включающий NHгруппу (i=1-4).4. Каталитическое покрытие по п. 1, отличающееся тем, что Г-катализатор содержит соединение, адсорбирующее ...

КАТАЛИТИЧЕСКАЯ СИСТЕМА И СПОСОБ ГИДРОПЕРЕРАБОТКИ ТЯЖЕЛЫХ МАСЕЛ

... 1. Каталитическая система, применяемая для гидропереработки тяжелых масел, отличающаяся тем, что она включает: ! а. катализатор, имеющий функцию катализатора гидрирования, содержащий МоS2 или WS2 или их смеси в форме пластинок, или их маслорастворимый предшественник; ! b. сокатализатор, включающий частицы наноразмеров или микронных размеров, выбранный из катализаторов крекинга и/или денитрификации. ! 2. Каталитическая система по п.1, в которой сокатализатор состоит из цеолитов, имеющих кристаллы небольших размеров и низкую степень агрегации первичных частиц, и/или оксидов или сульфидов, или предшественников сульфидов Ni, и/или Со, в смеси с Мо и/или W. !3. Каталитическая система по п.2, в которой цеолиты выбраны из группы, включающей цеолиты с промежуточными или крупными размерами пор. ! 4. Каталитическая система по п.3, в которой цеолиты с промежуточными или крупными размерами пор выбраны из бета-цеолита, цеолита Y и МСМ-22. ! 5. Каталитическая система по п.2, в которой сокатализатор, ...

КАТАЛИЗАТОР ДЛЯ ПИРОЛИЗА СЫРЬЯ

КАТАЛИЗАТОР ДЛЯ ХОЛОДНОГО ПУСКА И ЕГО ПРИМЕНЕНИЕ В ВЫХЛОПНЫХ СИСТЕМАХ

... 1. Катализатор для холодного пуска, содержащий: (1) цеолитовый катализатор, содержащий неблагородный металл, благородный металл, и цеолит; и (2) катализатор с нанесенным металлом платиновой группы, содержащий один или несколько металлов платиновой группы и один или несколько носителей из неорганических оксидов.2. Катализатор для холодного пуска по п. 1, в котором неблагородный металл выбран из группы, состоящей из железа, меди, марганца, хрома, кобальта, никеля, олова и их смесей.3. Катализатор для холодного пуска по п. 1, в котором неблагородным металлом является железо.4. Катализатор для холодного пуска по п. 1, в котором благородный металл выбран из группы, состоящей из платины, палладия, родия и их смесей.5. Катализатор для холодного пуска по п. 1, в котором благородным металлом является палладий.6. Катализатор для холодного пуска по п. 1, в котором цеолит выбран из группы, состоящей из бета-цеолита, фожазита, L-цеолита, ZSM-цеолита, SSZ-цеолита, морденита, шабазита, оффретита, эрионита ...

АЛЮМОСИЛИКАТНОЕ ИЛИ СИЛИКОАЛЮМОФОСФАТНОЕ МОЛЕКУЛЯРНОЕ СИТО/ОКТАЭДРИЧЕСКОЕ МОЛЕКУЛЯРНОЕ СИТО НА ОСНОВЕ МАРГАНЦА В КАЧЕСТВЕ КАТАЛИЗАТОРОВ ДЛЯ ОБРАБОТКИ ВЫХЛОПНЫХ ГАЗОВ

КАТАЛИЗАТОР ГИДРОКРЕКИНГА ДЛЯ ПРОИЗВОДСТВА СРЕДНИХ ДИСТИЛЛЯТОВ, СОДЕРЖАЩИЙ ЦЕОЛИТ USY И ЦЕОЛИТ БЕТА С НИЗКОЙ КИСЛОТНОСТЬЮ И БОЛЬШИМ РАЗМЕРОМ ДОМЕНОВ

ФИЛЬТР ДЛЯ ФИЛЬТРОВАНИЯ ВЕЩЕСТВА В ВИДЕ ЧАСТИЦ ИЗ ВЫХЛОПНЫХ ГАЗОВ, ВЫПУСКАЕМЫХ ИЗ ДВИГАТЕЛЯ С ПРИНУДИТЕЛЬНЫМ ЗАЖИГАНИЕМ

... 1. Фильтр для фильтрования вещества в виде частиц (ВВЧ) из выхлопных газов, выпускаемых из двигателя с принудительным зажиганием, который содержит пористую подложку, имеющую впускные поверхности и выпускные поверхности, при этом впускные поверхности отделены от выпускных поверхностей пористой структурой, содержащей поры первого среднего размера, причем пористая структура покрыта покрытием, содержащим множество твердых частиц, причем пористая структура пористой подложки с покрытием содержит поры второго среднего размера, и поры второго среднего размера меньше пор первого среднего размера.2. Фильтр по п.1, в котором первый средний размер пор пористой структуры пористой подложки составляет от 8 до 45 мкм.3. Фильтр по п.1, в котором количество покрытия составляет >0,50 г/дюйм.4. Фильтр по п.3, в котором количество покрытия составляет >1,00 г/дюйм.5. Фильтр по пп.1, 2, 3 или 4, содержащий поверхностное покрытие, при этом слой покрытия, по существу, покрывает поверхностные поры пористой структуры ...

Exhaust system for a vehicular positive ignition internal combustion engine

Positive ignition engine comprising an exhaust system including a filter therefor

Filtering particulate matter from exhaust gas

A filter for filtering particulate matter (PM) from exhaust gas emitted from a positive ignition engine comprises a porous substrate 10 having inlet and outlet surfaces, wherein the inlet surfaces are separated from the outlet surfaces by a porous structure containing pores 12 of a first mean pore size. The porous structure is coated with a catalytic washcoat 14 comprising a plurality of solid particles, wherein the porous structure of the washcoated porous substrate contains pores 16 of a second mean pore size. The second mean pore size is less than the first mean pore size. The catalytic washcoat is a hydrocarbon trap comprising at least one molecular sieve which is un-metallised. Alternatively, the molecular sieve is catalysed with a platinum group metal. The washcoat may substantially cover surface pores of the porous structure or may sit substantially within the porous structure of the porous substrate. An exhaust system comprising the filter, a positive ignition engine comprising ...

CATALYST ADDITIVES

Modified Y molecular sieve and preparation method and use thereof, supported catalyst, and hydrocracking method

METHOD FOR PRODUCING HYDROGENATION CATALYST

Method for producing hydrogenarion catalyst

Catalyst compositions and their use in hydrocarbonconversion processes

Method for producing hydrogenarion catalyst

Method for producing hydrogenarion catalyst

Method and apparatus for catalytic conversion of a composition

Verfahren, Vorrichtung, Katalysator und Verfahren zur Herstellung eines Katalysators zur katalytischen Umwandlung einer Stoffmischung enthaltend Glycerin in Propanole in einem Festbettreaktor (2), wobei Substrate des Katalysators anorganische Materialien und/oder Metalloxide aufweisen, dadurch gekennzeichnet, dass die Substrate einen Porendurchmesser an der Oberfläche zwischen 10 und 25 Ångström, bevorzugt zwischen 12 und 20 Ångström, besonders bevorzugt im Wesentlichen von 15 Ångström aufweisen.

Hydrocracking catalyst containing beta and Y zeolites, and process for its use to produce naphtha

Gasoline sulfur reduction catalyst for fluid catalytic cracking process

Gasoline sulfur reduction in fluid catalytic cracking

Production of liquid hydrocarbons

The invention relates to a method of preparing a supported catalyst, which method comprises the steps of; (i) providing a porous catalyst support comprising a framework having an internal pore structure comprising one or more pores which internal pore structure comprises a precipitant; (ii) contacting the catalyst support with a solution or colloidal suspension comprising a catalytically active metal such that, on contact with the precipitant, particles comprising the catalytically active metal are precipitated within the internal pore structure of the framework of the catalyst support. The invention also relates to supported catalysts made according to the above method, and to use of the catalysts in catalysing chemical reactions, for example in the Fischer Tropsch synthesis of hydrocarbons.

Catalyst compositions and their use in hydrocarbon conversion processes

CATALYST SYSTEM AND PROCESS FOR CONVERSION OF A HYDROCARBON FEED UTILIZING THE CATALYST SYSTEM

The present invention relates to a catalyst system comprising: i. a first layer of a hydrocarbon conversion catalyst, the hydrocarbon conversion catalyst comprising: a first composition comprising a platinum group metal on a solid support; and a second composition comprising a transition metal on an inorganic support; ii. a second layer comprising a cracking catalyst; and to a process for conversion of a hydrocarbon feed utilizing this catalyst system.

HYDROCRACKING CATALYST CONTAINING BETA AND Y ZEOLITES, AND PROCESS FOR ITS USE TO PRODUCE NAPHTHA

Increased yields of naphtha and increased catalyst activity are obtained in a hydrocracking process by the use of a catalyst containing a beta zeolite and a Y zeolite having a unit cell size from 24.38 to 24.50 angstrom. The catalyst has a relatively high amount of Y zeolite relative to beta zeolite.

MIDDLE DISTILLATE HYDROCRACKING CATALYST CONTAINING ZEOLITE BETA WITH LOW OD ACIDITY AND LARGE DOMAIN SIZE

A hydrocracking catalyst is provided comprising: a. from 0.5 to 10 wt% zeolite beta having an OD acidity of 20 to 400 µmol/g and an average domain size from 800 to 1500 nm2; b. from 0 to 5 wt% zeolite USY having an ASDI between 0.05 and 0.12; wherein a wt% of the zeolite beta is greater than the wt% of the zeolite USY; c. a catalyst support; and d. at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table. A process for hydrocracking using the hydrocracking catalyst to produce middle distillates is provided. A method for making the hydrocracking catalyst is also provided.

CATALYST AND PROCESS FOR HYDROCRACKING HYDROCARBON FRACTIONS

L'invention concerne un catalyseur d'hydrocraquage renfermant au moins un métal du groupe VIB, et/ou au moins un métal du groupe VIII de la classification périodique, une matrice alumine, du phosphore, éventuellement au moins un élément du groupe VIIA (fluor) et une zéolithe Y non désaluminée globalement de paramètre cristallin supérieur à 2,438 nm, de rapport SiO2/Al2O3 global inférieur à 8, de rapport SiO2/Al2O3 de charpente inférieur à 21 et supérieur au rapport SiO2/Al2O3 global. L'invention concerne également un procédé d'hydrocraquage avec ce catalyseur , notamment aux basses pressions de 7,5 à 11 MPa.

CATALYST AND PROCESS FOR HYDROCRACKING HYDROCARBON FRACTIONS

L'invention concerne un catalyseur d'hydrocraquage renfermant au moins un métal du groupe VIB, et/ou au moins un métal du groupe VIII de la classification périodique, une matrice alumine, du phosphore, éventuellement au moins un élémen t du groupe VIIA (fluor) et une zéolithe Y non désaluminée globalement de paramètr e cristallin supérieur à 2,438 nm, de rapport SiO2/Al2O3 global inférieur à 8, de rapport SiO2/Al2O3 de charpente inférieur à 21 et supérieur au rapport SiO2/Al2O3 global . L'invention concerne également un procédé d'hydrocraquage avec ce catalyseur, notamment aux basses pressions de 7,5 à 11 MPa.

METHODS FOR PREPARING AND FORMING OF APPLIED ACTIVE METAL CATALYSTS AND PRECURSORS

Композиция катализатора гидрокрекинга, способ его получения и процесс преобразования углеводородного сырья с его использованием

Композиция катализатора гидрокрекинга, которая содержит металлический компонент гидрогенизации, удерживаемый на носителе, включающем цеолит со структурой фоязита, который имеет размер элементарной ячейки в интервале от 24,10 до 24,40 Å, объемное соотношение (SAR) между диоксидом кремния и оксидом алюминия больше 12 и удельную поверхность, по крайней мере, 850 м2/г, измеренную ВЕТ-методом в соответствии со стандартной методикой ASTM D 4365-95 с применением адсорбции азота с величиной р/ро 0,03.

КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ ДЛЯ ГИДРОКРЕКИНГА И СПОСОБ ЕЕ ИЗГОТОВЛЕНИЯ

Изобретение предоставляет каталитическую композицию, которая содержит один или более металлов Группы VIb, один или более металлов Группы VIII, один или более цеолитов и может содержать тугоплавкий оксидный материал. Описано способ ее приготовления путем совместного осаждения, а также использование композиции в гидрокрекинге.

ADDITIVE FOR GAS-PHASE OXIDATIVE DESULFURIZATION CATALYSTS

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

Hydrocracking catalyst and preparation method thereof

Catalysts improved and their use in the processes of hydrocarbon conversion

CATALYST Of HYDROCRAQUAGE INCLUDING/UNDERSTANDING a ZEOLITE THERE NOT GLOBALEMENTDESALUMINEE, an ELEMENT OF GROUP VB, AND an ELEMENT PROMOTER CHOSEN IN LEGROUPE FORMS BY BORON, PHOSPHORUS AND SILICON

CATALYSEUR D'HYDROCRAQUAGE

L'INVENTION CONCERNE UN CATALYSEUR DONT LA PHASE ACTIVE EST A BASE D'AU MOINS UN METAL OU COMPOSE DE METAL DU GROUPE VIII ET D'EVENTUELLEMENT AU MOINS UN METAL OU COMPOSE DE METAL DU GROUPE VI DE LA CLASSIFICATION PERIODIQUE DES ELEMENTS ET DONT LE SUPPORT RESULTE DU MELANGE D'UNE ZEOLITHE ET D'UNE MATRICE A BASE D'ALUMINE OBTENUE PAR CARBONATION D'UN ALUMINATE ALCALIN. LE CATALYSEUR TROUVE UNE APPLICATION DANS L'HYDROCRAQUAGE DE COUPES PETROLIERES.

CATALYST CONTAINING ZEOLITE THERE NOT OVERALL DISALUMINATED, OF BORON AND/OR DESILICIUM AND PROCESS Of HYDROCRAQUAGE

METHOD FOR PREPARING ZEOLITE?BASED CATALYST COMPOSITION

Making middle distillates from paraffin charge produced by Fischer-Tropsch synthesis comprises implementing hydrocracking catalyst comprising hydrodehydrogenating metal and composite support formed by Y-type zeolite and silicon carbide

L'invention concerne un procédé de production de distillats moyens à partir d'une charge paraffinique produite par synthèse Fischer-Tropsch, mettant en oeuvre un catalyseur d'hydrocraquage/hydroisomérisation comprenant au moins un métal hydro-déshydrogénant choisi dans le groupe formé par les métaux du groupe VIB et du groupe VIII de la classification périodique et un composite formé par une zéolithe de type Y et du carbure de silicium SiC, ledit procédé opérant à une température comprise entre 270 et 400°C, une pression comprise entre 1 et 9 MPa, une vitesse volumique horaire comprise entre 0,5 et 5 h-1, un débit d'hydrogène ajusté pour obtenir un rapport de 400 à 1500 normaux litres d'hydrogène par litre de charge.

REFINING OF

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

L'invention concerne un procédé d'hydroraffinage avec un catalyseur renfermant au moins une matrice, une zéolithe Y partiellement amorphe, au moins un métal choisi dans le groupe formé par les métaux du groupe VIB et du groupe VIII de la classification périodique, au moins un élément choisi dans le groupe formé par le phosphore, le bore et le silicium éventuellement au moins un élément du groupe VIIA, et éventuellement au moins un élément du groupe VIIB.

CATALYST COMPOSITION FOR HYDROGENATION TREATMENT OF HYDROCARBON AND HYDROGENATION TREATMENT METHOD

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

CATALYST WITH AN ION-MODIFIED BINDER

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 ...

A method for producing cyclohexanone dimer

The present invention provides a method for producing cyclohexanone dimer comprising performing the cyclohexanone condensation reaction in a presence of solid acid catalyst to obtain the cyclohexanone dimer; wherein the solid acid catalyst comprises tungsten oxide and a carrier with Lewis acid sites and Brønsted acid sites. The method of present invention has an advantage of mild condition, fast reaction rate and high selectivity, thereby enhancing the value of the industrial application.

PROCESS FOR PRODUCTION OF GLYCOLIC ACID

A process for producing glycolic acid from carbon monoxide and formaldehyde, optionally in a solvent, using a catalyst comprising an acidic polyoxometalate compound insoluble in formaldehyde, glycolic acid and the optional solvent, wherein the insoluble acidic polyoxometalate compound has a concentration of acid sites of greater than 60 μmol g-1 on the external surface and/or has a Hammett Acidity value of less than -12.8.

METHOD FOR DECOMPOSING DINITROGEN MONOXIDE

Disclosed is a method for decomposing dinitrogen monoxide, wherein a gas containing dinitrogen monoxide is brought into contact with a fluid catalytic cracking (FCC) equilibrium catalyst for decomposing dinitrogen monoxide.

REGENERABLE COMPOSITE CATALYSTS FOR HYDROCARBON AROMATIZATION

A composite catalyst for aromatization of hydrocarbons includes a molecular sieve catalyst and metal dehydrogenation catalyst present as discrete catalysts in a physical admixture. The molecular sieve catalyst can be a zeolite and the metal dehydrogenation catalyst can be in the form of a nanostructure, such as zinc oxide nanopowder. The catalyst can convert hydrocarbon feedstocks, such as alkanes and alkenes, to aromatics and can be regenerated in-situ.

PROCESS FOR PRODUCING LIGHT NEUTRAL BASE OIL HAVING A HIGH VISCOSITY INDEX

A process is disclosed for producing light neutral base oil having VI greater than 120 comprising the steps of contacting a hydrocarbonaceous feedstock with a catalyst comprising a low acidity, highly dealuminated ultrastable Y zeolite and a catalytic amount of hydrogenation component to produce a converted fractionand an unconverted fraction boiling above 700°F; recovering at least a portion of the unconverted fraction; dewaxing at least a portion of the unconverted fraction; separating at leat a portion of the dewaxed unconverted fraction into a least a first distillate fraction and a second distillate fraction, said first distillate fraction comprising a lubricating base oil having a viscosity of from about 3 cSt to about 6 cSt at 100°C. and said second distillate fraction having a viscosity of greater than about 6 cSt at 100°C; and recovering at least a portion of the first distillate fraction.

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.

Hydrocarbon conversion process and catalysts

A process for converting hydrocarbon oils into products of low average molecular weight and lower average boiling point comprising contacting a hydrocarbon oil at elevated temperature and pressure in the presence of hydrogen with a catalyst comprising a modified Y zeolite having a unit cell size below 24.45 Å, a degree of crystallinity which is at least retained at increasing SiO2 /Al2 O3 molar ratios, a water adsorption capacity (at 25° C. and p/po value of 0.2) of at least 8% by weight of modified zeolite and a pore volume of at least 0.25 ml/g wherein between 10% and 60% of the total pore volume is made up of pores having a diameter of at least 8 nm, an amorphous cracking component, a binder and at least one hydrogenation component of a Group VI metal and/or at least one hydrogenation component of a Group VIII metal. The invention also relates to catalyst compositions suitable for use in said process.

CATALYST COMPRISING ULTRASTABLE ALUMINOSILICATES AND HYDROCARBON CONVERSION PROCESSES EMPLOYING SAME

HYDROCRACKING PROCESS USING A ZEOLITE MODIFIED BY BASIC TREATMENT

The present invention describes a hydrocracking and/or hydrotreatment process using a catalyst comprising an active phase containing at least one hydrogenating/dehydrogenating component selected from the group VIB elements and the non-precious elements of group VIII of the periodic table, used alone or in a mixture, and a support comprising at least one dealuminated zeolite Y having an overall initial atomic ratio of silicon to aluminium between 2.5 and 20, an initial weight fraction of extra-lattice aluminium atoms greater than 10%, relative to the total weight of aluminium present in the zeolite, an initial mesopore volume measured by nitrogen porosimetry greater than 0.07 ml·gand an initial crystal lattice parameter abetween 24.38 Å and 24.30 Å, said zeolite being modified by a) a stage of basic treatment comprising mixing said dealuminated zeolite Y with a basic aqueous solution, and at least one stage c) of thermal treatment. 110-. (canceled)11. A process for modifying a dealuminated zeolite Y comprising a) a stage of basic treatment comprising mixing said dealuminated zeolite Y with a basic aqueous solution , said basic aqueous solution being a solution of basic compounds selected from alkaline bases and strong non-alkaline bases , said stage a) being carried out at a temperature between 40 and 100° C. and for a duration between 5 minutes and 5 h and at least one stage c) of thermal treatment carried out at a temperature between 200 and 700° C.12. A modified dealuminated zeolite Y obtained by the process for modifying according to .13. A modified dealuminated zeolite Y according to characterized in that said zeolite has a final mesopore volume measured by nitrogen porosimetry at least 10% greater relative to the initial mesopore volume of the dealuminated initial zeolite USY claim 12 , a final micropore volume measured by nitrogen porosimetry that must not decrease by more than 40% claim 12 , relative to the initial micropore volume of said dealuminated ...

Gasoline sulfur reductions catalyst for fluid catalytic cracking process

The invention is a composition that is suitable for reducing sulfur species from products produced by petroleum refining processes, especially gasoline products produced by fluidized catalytic cracking (FCC) processes. The composition comprises zeolite, yttrium, and at least one element selected from the group consisting of magnesium and manganese. The yttrium and the element are present (i) as cations exchanged onto the zeolite, and optionally (ii) in pores of the catalyst matrix. The zeolite is preferably a zeolite Y.

Sulphur reduction catalyst additive composition in fluid catalytic cracking and method of preparation thereof

The present invention relates to sulphur reduction catalyst additive composition comprising an inorganic porous support incorporated with metals; an alumino silicate or zeolite component; an alumina component and clay. More particularly the present invention relates to sulphur reduction catalyst additive composition comprising refinery spent catalyst as support. The primary sulphur reduction catalyst additive component of the catalyst composition contains metals of Group I, II, III, IV, V, VIII of the Periodic Table, preferably Zinc or Magnesium or combination thereof or one of the transition metals along with other metals.

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

Hydrocarbon conversion catalysts

MODIFIED ULTRA-STABLE Y (USY) ZEOLITE CATALYST FOR DEALKYLATION OF AROMATICS

КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ ДЛЯ ГИДРОКРЕКИНГА И СПОСОБ ПРЕВРАЩЕНИЯ УГЛЕВОДОРОДНОГО СЫРЬЯ В НИЗКОКИПЯЩИЕ МАТЕРИАЛЫ

Настоящее изобретение относится к каталитическим композициям и их использованию в гидрокрекинге. Описана каталитическая композиция для гидрокрекинга, включающая носитель, содержащий цеолит фожазитной структуры с размером элементарной ячейки в интервале 24,10-24,40 Å, объемным соотношением оксид кремния : оксид алюминия (SAR) около 12 и площадью поверхности, по меньшей мере, 850 м2/г согласно измерению методом BET и ASTM D 4365-95 по адсорбции азота при значении р/ро 0,03, и объемом микропор, по меньшей мере, 0,28 мл/г, гидрирующий компонент - по меньшей мере, один металл, выбранный из металлов VIB и VIII группы Периодической системы элементов Менделеева, и необязательно, связующее вещество. Каталитическая композиция получена способом, включающим a) приготовление исходного цеолита фожазитной структуры с соотношением между оксидом кремния и оксидом алюминия в интервале 4,5-6,5 и содержанием щелочи менее 1,5 мас.%; b) гидротермальную обработку указанного исходного цеолита при температуре 600 ...

КАТАЛИЗАТОР, СОДЕРЖАЩИЙ ПО МЕНЬШЕЙ МЕРЕ ОДИН ЦЕОЛИТ NU-86, ПО МЕНЬШЕЙ МЕРЕ ОДИН ЦЕОЛИТ USY И ПОРИСТУЮ НЕОРГАНИЧЕСКУЮ МАТРИЦУ, И СПОСОБ ГИДРОКОНВЕРСИИ УГЛЕВОДОРОДНОГО СЫРЬЯ С ИСПОЛЬЗОВАНИЕМ ЭТОГО КАТАЛИЗАТОРА

Изобретение относится к катализатору гидрокрекинга углеводородного сырья, содержащему по меньшей мере один металл, выбранный из группы, состоящей из металлов группы VIB и группы VIII периодической системы, используемых по отдельности или в смеси, и подложки, содержащей по меньшей мере один цеолит NU-86, по меньшей мере один цеолит Y и по меньшей мере одну неорганическую пористую матрицу, содержащую по меньшей мере алюминий и/или по меньшей мере кремний, причем указанный катализатор содержит, мас.% от общей массы катализатора: 0,2-10 по меньшей мере одного цеолита NU-86, 0,4-40 по меньшей мере одного цеолита Y, 0,5-50 по меньшей мере одного гидрирующего-дегидрирующего металла, выбранного из группы, состоящей из металлов группы VIB и группы VIII, 1-99 по меньшей мере одной неорганической пористой матрицы, содержащей по меньшей мере алюминий и/или по меньшей мере кремний. Изобретение относится также к способу гидрокрекинга углеводородного сырья с использованием указанного катализатора. Технический ...

КАТАЛИЗАТОР ГИДРОКРЕКИНГА, СОДЕРЖАЩИЙ БЕТА- И Y ЦЕОЛИТЫ, И СПОСОБ ЕГО ПРИМЕНЕНИЯ ДЛЯ ПОЛУЧЕНИЯ НАФТЫ

Настоящее изобретение относится к способу гидрокрекинга углеводородного сырья. Способ включает введение в контакт сырья при температуре от 232°С до 454°С и избыточном давлении от 5171 кПа(и) до 24132 кПа(и) в присутствии водорода с катализатором, содержащим носитель, гидрирующий компонент, бета-цеолит и Y цеолит, имеющий размер элементарной ячейки от 24,38 до 24,50 ангстрем, предпочтительно от 24,40 до 24,44 ангстрем. Катализатор имеет весовое отношение Y-цеолита к бета-цеолиту в сухом состоянии от 5 до 12, при этом суммарное содержание бета-цеолита и Y цеолита составляет, по меньшей мере, 40% масс. в расчете на объединенный вес бета-цеолита, Y цеолита и носителя в сухом состоянии. Также предложена композиция вещества для гидрокрекинга углеводородного сырья. Изобретение позволяет повысить выход нафты и получить катализатор с повышенной активностью. 2 н. и 8 з.п. ф-лы, 1 табл.

КАТАЛИЗАТОР ГИДРОКРЕКИНГА

... 1. Способ получения носителя катализатора гидрокрекинга, содержащего аморфный связующий компонент и цеолит Y, который включает в себя прокаливание цеолита Y с мольным отношением диоксида кремния к оксиду алюминия по меньшей мере равным 10, при температуре от 700 до 1000°С.2. Способ по п.1, который включает в себя прокаливание смеси аморфного связующего компонента и цеолита Y с мольным отношением диоксида кремния к оксиду алюминия по меньшей мере равным 10, при температуре от 700 до 1000°С.3. Способ по п.1 или 2, в котором смесь дополнительно содержит цеолит бета.4. Способ по п.1, который включает в себя прокаливание цеолита Y с мольным отношением диоксида кремния к оксиду алюминия по меньшей мере равным 10, при температуре от 700 до 1000°С и последующее смешивание полученного цеолита Y с аморфным связующим компонентом и, необязательно, цеолитом бета.5. Способ по любому пп.1 или 2, в котором носитель содержит от 2 до 70% масс. цеолита и от 98 до 30% масс. аморфного связующего компонента.6 ...

ВЫСОКОСЕЛЕКТИВНЫЙ КАТАЛИЗАТОР ДЛЯ ПРОИЗВОДСТВА ФРАКЦИЙ ВЫСОКОКАЧЕСТВЕННОГО БЕНЗИНА ИЗ СИНТЕЗ-ГАЗА И СПОСОБ ЕГО ИЗГОТОВЛЕНИЯ

... 1. Высокоселективный катализатор для производства фракций высококачественного бензина из синтез-газа, состоящий из кобальта, промотора и молекулярного сита, в котором массовое содержание кобальта составляет 1-30%, массовое содержание промотора составляет 0,01-5%, а остальная часть представляет собой молекулярное сито.2. Катализатор по п.1, отличающийся тем, что содержание кобальта составляет 8-15%, а содержание промотора составляет 0,05-2%.3. Катализатор по п.2, отличающийся тем, что молекулярное сито представляет собой одно или несколько молекулярных сит, выбранных среди молекулярных сит Beta, ZSM-5, MOR, Y и МСМ-22, причем предпочтительно отношение Si/Al у молекулярного сита составляет от 5 до 300, более предпочтительно молекулярное сито представляет собой молекулярное сито Beta и/или ZSM-5, имеющее отношение Si/Al в диапазоне от 20 до 100.4. Катализатор по п.3, отличающийся тем, что кислотность молекулярного сита выражается через количество адсорбированного NHи адсорбционная способность ...

КАТАЛИЗАТОР ГИДРОКРЕКИНГА СРЕДНИХ ДИСТИЛЛЯТОВ, СОДЕРЖАЩИЙ ВЫСОКОСТАБИЛИЗИРОВАННЫЙ ЦЕОЛИТ Y С УЛУЧШЕННЫМ РАСПРЕДЕЛЕНИЕМ КИСЛОТНЫХ ЦЕНТРОВ

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 35/00 B01J 35/10 B01J 29/10 B01J 29/16 C01B 39/24 C10G 47/20 ФЕДЕРАЛЬНАЯ СЛУЖБА B01J 37/20 ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ B01J 35/02 (12) (11) (13) 2017 118 406 A (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2017118406, 28.07.2015 (71) Заявитель(и): ШЕВРОН Ю.Эс.Эй. ИНК. (US) Приоритет(ы): (30) Конвенционный приоритет: 31.10.2014 US 14/529,794 34 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 31.05.2017 US 2015/042355 (28.07.2015) (87) Публикация заявки PCT: R U Адрес для переписки: 129090, Москва, ул. Б.Спасская, 25, строение 3, ООО "Юридическая фирма Городисский и Партнеры" (54) КАТАЛИЗАТОР ГИДРОКРЕКИНГА СРЕДНИХ ДИСТИЛЛЯТОВ, СОДЕРЖАЩИЙ ВЫСОКОСТАБИЛИЗИРОВАННЫЙ ЦЕОЛИТ Y С УЛУЧШЕННЫМ РАСПРЕДЕЛЕНИЕМ КИСЛОТНЫХ ЦЕНТРОВ (57) Формула изобретения 1. Катализатор гидрокрекинга, содержащий: носитель; аморфный кремнезем-глиноземистый материал; стабилизированный цеолит Y, имеющий величину индексного показателя распределения кислотных центров от 0,02 до 0,12; и по меньшей мере один металл, выбранный из группы, состоящей из элементов группы 6 и групп 8-10 Периодической таблицы элементов. 2. Катализатор по п. 1, отличающийся тем, что стабилизированный цеолит Y представляет собой стабилизированный цеолит Y с высоким объемом нанопор, имеющий объем нанопор в диапазоне размеров от 20 до 50 нм, от 0,15 до 0,6 куб.см/г. 3. Катализатор по п. 2, отличающийся тем, что от 20 до 30% нанопор имеют размеры в диапазоне от 8 до 20 нм. 4. Катализатор по п. 2, отличающийся тем, что от 40 до 60% нанопор имеют размеры в диапазоне от 20 до 50 нм. 5. Катализатор по п. 2, отличающийся тем, что от 15 до 25% нанопор имеют размеры более 50 нм. Стр.: 1 A 2 0 1 7 1 1 8 4 0 6 A WO 2016/069071 (06.05.2016) 2 0 1 7 1 1 8 4 0 6 (86) Заявка PCT: R U (43) Дата публикации заявки: 04.12.2018 Бюл. № (72) Автор(ы): ЧЖАН Ихуа (US), МАЭСЕН Теодорус Людовикус Майкл (US), ЛАЧИН Ховард ...

КАТАЛИЗАТОР ГИДРОКРЕКИНГА ДЛЯ ПРОИЗВОДСТВА СРЕДНИХ ДИСТИЛЛЯТОВ, СОДЕРЖАЩИЙ ЦЕОЛИТ БЕТА С НИЗКОЙ КИСЛОТНОСТЬЮ OD И БОЛЬШИМ РАЗМЕРОМ ДОМЕНОВ

КАТАЛИЗАТОР УМЕНЬШЕНИЯ СОДЕРЖАНИЯ СЕРЫ В БЕНЗИНЕ ДЛЯ ПРОЦЕССА КАТАЛИТИЧЕСКОГО КРЕКИНГА В ЖИДКОЙ ФАЗЕ

... 1. Крекирующая каталитическая композиция, пригодная для эксплуатации в установке с псевдоожиженным катализатором крекинга, используемой для крекинга углеводородного сырья, содержащего органические производные серы, включающая (a) цеолит и (b) компонент, содержащий кислоту Льюиса, причем рассматриваемая каталитическая композиция дополнительно содержит Na2O в количестве 0,20 мас.% или менее. 2. Композиция по п.1, содержащая Na2O в количестве 0,15 мас.% или менее. 3. Композиция по п.1, содержащая Na2O в количестве 0,10 мас.% или менее 4. Композиция по п.1, в котором цеолит (а) содержит Na2O в количестве 0,5 мас.% или менее. 5. Композиция по п.1, в котором цеолит (а) содержит Na2O в количестве 0,3 мас.% или менее. 6. Композиция по п.1, в котором цеолит (а) содержит Na2O в количестве 0,1 мас.% или менее. 7. Композиция по п.1, в котором компонент (b), включающий кислоту Льюиса, содержит Na2O в количестве 0,1 мас.% или менее. 8. Композиция по п.1, в котором цеолит представляет собой цеолит Y-типа ...

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА ГИДРОКРЕКИНГА

... 1. Способ получения катализатора гидрокрекинга, который включает стадии:(a) перемешивания цеолита Y, характеризующегося размером элементарной ячейки в диапазоне от 24,42 до 24,52 Å, молярным соотношением между диоксидом кремния и оксидом алюминия (SAR) в диапазоне от 10 до 15 и площадью удельной поверхности в диапазоне от 910 до 1020 м/г, со связующим компонентом на основе оксида алюминия и двумя или более каталитически активными металлсодержащими компонентами, где данные металлсодержащие компоненты содержатся в одном или более растворах, где цеолит Y присутствует в количестве, составляющем 40% (масс.) или более, при расчете на совокупную массу цеолита Y и связующего компонента на основе оксида алюминия;(b) экструдирования смеси, полученной на стадии (а);(c) высушивания экструдированной смеси, полученной на стадии (b);(d) прокаливания высушенной и экструдированной смеси, полученной на стадии (с); и(e) перемешивания прокаленного продукта, полученного на стадии (d), с двумя или более каталитически ...

Катализатор для гидрокрекинга тяжелого углеводородного нефтепродукта и способ гидрокрекинга тяжелого углеводородного нефтепродукта

Изобретение относится к нефтехимии , в частности к катализатору для гидрокрекинга тяжелого углеводородного нефтепродукта и к способу гидрокрекинга Цель - повышение селективности катализатора по средним дистиллятам и повышение выхода средних дистиллятов о Катализатор имеет следу- ющее соотношение компонентов, мас.%: модифицированный цеолит У 67,0-79,4, гидрирующий компонент - оксид никеля 3,3-5,0 и оксид молибдена или вольфрама 6,3-10,3 или платина и палладий 0,8, оксид алюминия остальное. Используют модифицированный цеолит с элементарными ячейками 24,32-24,33 А. со степенью кристалличности, сохраняющейся при увеличении молярного отношения диоксида кремния к оксиду алюминия, с водоадсорбционной способностью при 25°С и значении Р/Р 0,2, где Р - парциальное давление паров воды, №а, Ра - давление насыщения воды при 25°С, МПа, равной 10,6- 11,3 мас.% с объемом пор 0,4-0,47 мл/г, причем 18-27% объема пор составляют поры диаметром более 8 нм. Гидрокрекинг проводят путем контактирования тяжелого ...

Verfahren zur Herstellung eines Hydroentschwefelungskatalysator

Filter

Procedure for the shifting of hydrocarbons

Katalysator

Katalysator aufweisend eine Heteropolysäure, wobei das Substrat des Katalysators anorganische Materialien und/oder Metalloxide aufweist, wobei die Heteropolysäure als korrespondierendes Lakunarion der ursprünglichen Keggin-Struktur vorliegt und dass das Substrat des Katalysators einen Porendurchmesser an der Oberfläche zwischen 5 und 20 Ångström aufweist. Weiters ein Verfahren zur Herstellung eines solchen Katalysators. Weiters eine Vorrichtung und ein Verfahren zur katalytischen Umwandlung einer Stoffmischung enthaltend Glycerin, vorzugsweise Rohglycerin, in Propanole in einem Festbettreaktor.

CRACKING CATALYST FOR HYDROCARBONS, WHICH ARE CONTAMINATED WITH VANADIUM.

PROCESS FOR HYDROCRACKING OF A HYDROCARBON FEEDSTOCK

Method for producing hydrogenation catalyst

A method for producing a hydrogenation catalyst which comprises: a loading step wherein a carrier, which contains a carbonaceous substance containing a carbon atom in an amount of 0.5% by mass or less in terms of carbon atoms, is loaded with an active metal component that contains at least one active metal element selected from among group 6 metals, group 8 metals, group 9 metals and group 10 metals of the periodic table so as to obtain a catalyst precursor; and a firing step wherein the catalyst precursor obtained in the loading step is fired so as to obtain a hydrogenation catalyst.

A multifunctional catalyst additive composition and process of preparation thereof

The present invention relates to a multifunctional catalyst additive composition for reduction of carbon monoxide and nitrogen oxides in a fluid catalytic cracking process comprising an inorganic oxide; alumino silicate or a zeolite; a noble metal; a metal of Group I A; a metal of Group II A; a metal of Group III A; a metal of Group IV A; a metal of Group V A; a rare earth oxide; at least a metal of Group VIII. The composition is attrition resistant and is incorporated on a support. The present invention also discloses a process for preparing the multifunctional catalyst additive composition. The present invention also discloses a fluid cracking catalyst comprising the multifunctional catalyst additive composition. sa b -10 10 30 50 70 90 110 130 150 170 190 210 230 250 270 290 310 PSD, A Figure-1 Comparision of pore size distribution of different supports a,b,c are different supports used for making catalyst additives.

MIDBARREL HYDROCRACKING

Certain hydrophobic derivatives of zeolite Y are found to unusually selective and active catalysts with adequate stability for use in the conversion high boiling petroleum feedstocks into fuel gases, gasoline and middle distillate products such as diesel and turbine fuel.

MIDDLE DISTILLATE HYDROCRACKING CATALYST CONTAINING ZEOLITE USY, AND ZEOLITE BETA WITH LOW ACIDITY AND LARGE DOMAIN SIZE

A hydrocracking catalyst is provided comprising: a zeolite beta having an OD acidity of (20) to (50) µm?l/g and an average crystal size from (300) to (800) nanometers; a zeolite USY; wherein a wt% of the zeolite beta is less than the wt% of the zeolite USY; a support comprising an amorphous silica aluminate and a second support material; and at least one metal selected from the group consisting of elements from Group (6) and Groups (8) through (10) of the Periodic Table. A process for hydrocracking a hydrocarbonaceous feedstock is provided, comprising: contacting the hydrocarbonaceous feedstock with the hydrocracking catalyst under hydrocracking conditions to produce a hydrocracked effluent that comprises middle distillates. A method for making the hydrocracking catalyst is also provided.

MIDDLE DISTILLATE HYDROCRACKING CATALYST CONTAINING HIGHLY A STABILIZED Y ZEOLITE WITH ENHANCED ACID SITE DISTRIBUTION

MODIFIED Y-TYPE MOLECULAR SIEVE AND PREPARATION METHOD THEREOF, HYDROCRACKING CATALYST AND PREPARATION METHOD THEREOF, AND METHOD FOR HYDROCRACKING HYDROCARBON OIL

A modified Y-type molecular sieve and a preparation method therefor, a hydrocracking catalyst and a preparation method therefor, and a method for hydrocracking hydrocarbon oil. Based on the total weight of the modified Y-type molecular sieve, the modified Y-type molecular sieve contains 0.5-2 wt% of Na2O, the ratio of the total IR acid amount of pyridine of the modified Y-type molecular sieve to the total IR acid amount of N-butyl pyridine of the modified Y-type molecular sieve is 1-1.2, and the total IR acid amount of pyridine of the modified Y-type molecular sieve is 0.1-1.2 mmol/g. The molecular sieve acid center sites of the modified Y-type molecular sieve are distributed mainly in macropores. Applying the molecular sieve to the hydrocracking reaction process of wax oil facilitates improving reaction selectivity of macromolecular cyclic hydrocarbons in the wax oil, reducing occurrence of secondary cracking reaction, improving the quality of hydrocracking unconverted oil, and increasing ...

CATALYST COMPOSITION REDUCING GASOLINE SULFUR CONTENT IN CATALYTIC CRACKING PROCESS

A sulfur reduction catalyst useful to reduce the levels of sulfur in a cracked gasoline product comprises a metal vanadate compound. The metal vanadate compound can be supported on a molecular sieve such as a zeolite in which the metal vanadate compound is primarily located on the exterior surface of the pore structure of the zeolite and on the surface of any matrix material used to bind or support the zeolite.

CATALYTIC SYSTEM AND PROCESS FOR THE HYDROCONVERSION OF HEAVY OIL PRODUCTS

Catalytic system which can be used in processes for the hydroconversion of heavy oils by means of hydrotreatment in slurry phase, characterized in that it comprises: a catalyst, having the function of hydrogenating agent, containing MoS2 or WS2 or mixtures thereof in lamellar form or an oil-soluble precursor thereof; a co-catalyst, having nanometric or micronic particle- sizes, selected from cracking and/or denitrogenation catalysts. The co-catalyst preferably consists of zeolites having small-sized crystals and with a low aggregation degree between the primary particles, and/or oxides or sulfides or precursors of sulfides of Ni and/or Co in a mixture with Mo and/or W.

SUPPORTED CATALYSTS FOR PRODUCING ULTRA-LOW SULPHUR FUEL OILS

The present invention relates to the preparation of catalysts used in the hydrodesulfurisation of fossil fuels and proposes a method for preparing thermally stable, low-cost catalysts for the hydrodesulfurisation of petrol and diesel, based on highly active CoMo and NiMo. The catalyst for the hydroprocessing of gas oil or petrol in the present invention comprises a precursor which consists of chemical compounds obtained from organic acids and metal salts and a support containing an ultra-stable Y-type zeolite useful in the hydroprocessing of heavy gas oil and/or light cyclic gas oil with high conversion rates.

PROCESS FOR PREPARING AN INDUSTRIAL HYDROCONVERSION CATALYST, CATALYST THUS OBTAINED AND USE THEREOF IN A HYDROCONVERSION PROCESS

La présente invention a pour objet un procédé pour la préparation d'un catalyseur d'hydroconversion à base de zéolithe modifiée Y, comprenant les étapes . A- de préparation d'une zéolithe modifiée Y, dont la structure intracristalline présente au moins un réseau de micropores, au moins un réseau de petits mésopores ayant un diamètre moyen de 2 à 5 nm et au moins un réseau de grands mésopores ayant un diamètre moyen de 10 à 50 nm, ces différents réseaux étant interconnectés; B- de mélange de la zéolithe avec un liant, de mise en forme du mélange et ensuite de calcination, C- d'introduction d'au moins un métal catalytique choisi parmi les métaux du groupe VIII et/ou du groupe VIB, suivie par la calcination. La présente invention concerne aussi un catalyseur obtenu par l'intermédiaire de ce procédé et également son utilisation ...

METHOD FOR PRODUCING HYDROGENATION CATALYST

A method for producing a hydrogenation catalyst which comprises: a loading step wherein a carrier, which contains a carbonaceous substance containing a carbon atom in an amount of 0.5% by mass or less in terms of carbon atoms, is loaded with an active metal component that contains at least one active metal element selected from among group 6 metals, group 8 metals, group 9 metals and group 10 metals of the periodic table so as to obtain a catalyst precursor; and a firing step wherein the catalyst precursor obtained in the loading step is fired so as to obtain a hydrogenation catalyst.

METHODS OF PREPARATION AND FORMING SUPPORTED ACTIVE METAL CATALYSTS AND PRECURSORS

CATALYST HYDRO CRACKING FOR LIQUID PETROLEUM PRODUCT, METHOD OF PREPARING CATALYST HYDRO CRACKING AND METHOD HYDRO CRACKING LIQUID PETROLEUM PRODUCT WITH THE HELP OF CATALYST HYDRO CRACKING

СПОСОБ И КАТАЛИЗАТОР ДЛЯ ПОЛУЧЕНИЯ ЛИНЕЙНЫХ АЛКАНОВ

Изобретение относится к способу получения линейных алканов, содержащих менее 6 атомов углерода, из смеси, включающей один или более углеводородов, содержащих по меньшей мере 6 атомов углерода. В способе используют каталитическую композицию, включающую определённые комбинации цеолита Y-типа, по меньшей мере одного элемента, выбранного из Zn, Mo, Cu, Ga, In, W, Ta, Zr, Ti, металлов VIII группы и, возможно, одного или более лантаноидов.

METHOD OF PREPARING CATALYST HYDRO GENIZATsII

Mesoporous y hydrocracking catalyst and associated hydrocracking processes

This invention relates to the composition, method of making and use of a hydrocracking catalyst that is comprised of a new Y zeolite which exhibits an exceptionally low small mesoporous peak around the 40 Å (angstrom) range as determined by nitrogen adsorption measurements. The hydrocracking catalysts of invention exhibit improved distillate yield and selectivity as well as improved conversions at lower temperatures than conventional hydrocracking catalysts containing Y zeolites. The hydrocracking catalysts herein are particularly useful in the hydrocracking processes as disclosed herein, particularly for conversion of heavy hydrocarbon feedstocks such as gas oils and vacuum tower bottoms and an associated maximization and/or improved selectivity of the distillate yield obtained from such hydrocracking processes.

MESOSTRUCTURED ZEOLITIC MATERIALS SUITABLE FOR USE IN HYDROCRACKING CATALYST COMPOSITIONS AND METHODS OF MAKING AND USING THE SAME

Hydrocracking processes and catalyst composition for use therein are provided. The catalyst compositions described herein include a mesoporous support material and at least one catalytic metal supported thereon. The mesoporous support material may comprise a single-phase crystalline mesostructured zeolite. Additionally, the mesoporous structure may exhibit long range crystallinity and include a plurality of mesopores defined within of the volume of the crystalline mesostructure. Suitable feedstocks for the hydrocracking processes according to embodiments of the present invention crude oil, a gas oil fraction, vacuum gas oil, and combinations thereof. 1. A hydrocracking process comprising: contacting said hydrocarbon-containing feedstock with a catalyst composition under hydrocracking conditions to thereby produce a hydrocracked product , wherein said catalyst composition comprises a mesoporous support material and at least one catalytic metal supported thereon , wherein said mesoporous support material comprises a mesostructured crystalline inorganic one-phase hybrid single crystal material having long-range crystallinity and comprising a plurality of mesopores.2. The hydrocracking process of claim 1 , wherein said crystalline inorganic material is a zeolite.3. The hydrocracking process of claim 1 , wherein said mesopores are configured in an arranged pattern claim 1 , wherein the arranged pattern produces one or more distinctive XRD peaks at two theta values between 0 and 8 two theta angle degrees and one or more distinctive XRD peaks at two theta values between 0 and 8 two theta angle degrees higher than 8.4. The hydrocracking process of claim 1 , wherein said crystalline inorganic material has the structure of a faujasite (FAU) claim 1 , mordenite (MOR) claim 1 , or ZSM-5 (MFI).5. The hydrocracking process of claim 1 , wherein said crystalline inorganic material has a total mesoporous adsorption volume of at least 0.05 cubic centimeters per gram (cc/g).6. The ...

PROCESS FOR PREPARING AN INDUSTRIAL HYDROCONVERSION CATALYST, CATALYST THUS OBTAINED AND USE THEREOF IN A HYDROCONVERSION PROCESS

The invention relates to a process for preparing a hydroconversion catalyst based on modified zeolite Y, comprising the steps of:

CATALYTIC REDUCTION OF NOx WITH HIGH ACTIVITY CATALYSTS WITH NH3 REDUCTANT

Methods and systems for selective catalytic reduction of NOx with an ammonia reductant and a zeolite catalyst loaded with at least two metals selected from the group of tungsten, cobalt, and vanadium. An exhaust stream including NOx and a reductant stream including ammonia are provided to a catalytic reactor having the metal loaded zeolite catalyst at suitable operating temperatures for NOx reduction of at least 90%. 1. A method for selective catalytic reduction of NOx comprising:providing an exhaust stream from a combustion operation, the exhaust stream containing an amount of NOx;introducing at least a portion of the exhaust stream and a reductant stream including ammonia to a catalytic reactor comprising a zeolite catalyst loaded with at least two metals selected from the group consisting of tungsten, cobalt, and vanadium, the reductant stream and the at least a portion of the exhaust stream being introduced to the catalytic reactor at suitable operating conditions to reduce the amount of NOx in the exhaust stream; anddirecting the NOx-reduced exhaust stream from the catalytic reactor.2. The method of claim 1 , wherein the exhaust stream includes between about 0.1% and about 20% oxygen and between about 1% and about 10% water.3. The method of claim 1 , wherein providing the reductant stream comprises providing a molar ratio of ammonia to NOx between 0.5:1 and 1.5:1 in the catalytic reactor.4. The method of claim 1 , wherein providing the reductant stream comprises providing between 5 ppm and 2000 ppm of ammonia.5. The method of claim 1 , wherein introducing the reductant stream and the at least a portion of the exhaust stream collectively have a gaseous hourly space velocity of between 5K cc per hour and 120K cc per hour through the catalytic reactor.6. The method of claim 1 , wherein the operating temperature of the at least one catalytic reactor is between about 250° C. and about 400° C.7. The method of claim 1 , wherein the exhaust stream is provided from at ...

HONEYCOMB DENITRATION CATALYST FOR FLUE GAS AT 400°C-600°C AND PREPARATION METHOD THEREOF

A honeycomb denitration catalyst used for flue gas at 400° C.-600° C. and preparation method thereof. The honeycomb denitration catalyst includes a catalyst coating and a honeycomb ceramic, where a slurry of the catalyst coating is made from components having the following mass percentages: 15%-25% of a zeolite, 5%-10% of a γ-alumina, 5%-10% of a catalyst auxiliary agent, 5% of a binder, and 50%-70% of deionized water. The honeycomb ceramic is soaked repeatedly into the slurry of the catalyst coating. After the soaking is completed, the obtained product is dried and calcined to obtain the honeycomb denitration catalyst. The honeycomb denitration catalyst contains a catalyst auxiliary agent and has excellent denitration activity at high temperatures, sulphur-resistance and water-tolerance ability, stability and NOremoving ability. 1. A honeycomb denitration catalyst used for flue gas at 400° C.-600° C. , comprising a catalyst coating and a honeycomb ceramic , wherein the catalyst coating is deposited on surfaces of the honeycomb ceramic , the catalyst coating is made from components having the following mass percentages:a zeolite in an amount of 15%-25%;a γ-alumina in an amount of 5%-10%;a catalyst auxiliary agent in an amount of 5%-10%;a binder in an amount of 5%; anddeionized water in an amount of 50-70%.2. The honeycomb denitration catalyst of claim 1 , wherein the catalyst coating is 2%-15% of the total mass of the honeycomb denitration catalyst.3. The honeycomb denitration catalyst of claim 1 , wherein the zeolite is selected from the group consisting of ZSM-5 type zeolite molecular sieve claim 1 , A-type zeolite molecular sieve claim 1 , X-type zeolite molecular sieve claim 1 , Y-type zeolite molecular sieve claim 1 , and any combinations thereof4. The honeycomb denitration catalyst of claim 1 , wherein the catalyst auxiliary agent is selected from the group consisting of ammonium molybdate claim 1 , cerium nitrate claim 1 , ferrous chloride claim 1 , ammonium ...

PROCESSING OF PARAFFINIC NAPHTHA WITH MODIFIED USY ZEOLITE DEHYDROGENATION CATALYST

Methods for processing paraffinic naphtha include contacting a paraffinic naphtha feedstock with a catalyst system in a dehydrogenation reactor. The catalyst system includes a framework-substituted ultra-stable Y (USY)-type zeolite to produce a dehydrogenated product stream. The catalyst system includes a framework-substituted ultra-stable Y (USY)-type zeolite. The framework-substituted USY-type zeolite has a modified USY framework. The modified USY framework includes a USY aluminosilicate framework modified by substituting a portion of framework aluminum atoms of the USY aluminosilicate framework with substitution atoms independently selected from the group consisting of titanium atoms, zirconium atoms, hafnium atoms, and combinations thereof. A dehydrogenation catalyst for dehydrogenating a paraffinic naphtha includes the framework-substituted ultra-stable Y (USY)-type zeolite. 2. The method of claim 1 , wherein the framework-substituted USY-type zeolite contains from 0.01% to 5% by mass substitution atoms claim 1 , as calculated on an oxide basis claim 1 , based on the total mass of the framework-substituted USY-type zeolite.3. The method of claim 1 , wherein:the framework-substituted USY-type zeolite contains from 0.01% to 5% by mass substitution atoms, as calculated on an oxide basis, based on the total mass of the framework-substituted USY-type zeolite; andthe substitution atoms comprise a combination selected from the group consisting of (a) titanium atoms and zirconium atoms, (b) titanium atoms and hafnium atoms, (c) zirconium atoms and hafnium atoms, and (d) titanium atoms, zirconium atoms, and hafnium atoms.4. The method of claim 1 , wherein:the framework-substituted USY-type zeolite contains from 0.01% to 5% by mass substitution atoms, as calculated on an oxide basis, based on the total mass of the framework-substituted USY-type zeolite; andthe substitution atoms comprise titanium atoms and zirconium atoms.5. The method of claim 1 , wherein the ...

FIBROUS ZEOLITE CATALYST FOR HYDROCRACKING

A hydrocracking catalyst for petroleum hydrocracking is provided, the hydrocracking catalyst provided in a form of at least one fiber, and the at least one fiber comprising at least one zeolite and at least one metal oxide. Methods are also provided to form the hydrocracking catalyst in the form of at least one fiber, particularly electrospinning. 1. A hydrocracking catalyst for petroleum hydrocracking , comprising:the hydrocracking catalyst provided in a form of at least one fiber; andthe at least one fiber comprising at least one zeolite and at least one metal oxide.2. The catalyst of claim 1 , wherein:the at least one zeolite is a Y-zeolite.3. The catalyst of claim 2 , wherein:{'sub': 2', '2', '3, 'the Y-zeolite has a SiO/AlOmole ratio of at least 3 to 1.'}4. The catalyst of claim 1 , wherein:the at least one metal oxide is one of nickel oxide and tungsten trioxide.5. The catalyst of claim 1 , wherein:the at least one metal oxide further comprises at least a first metal oxide and a second metal oxide.6. The catalyst of claim 5 , wherein:the first metal oxide is nickel oxide; andthe second metal oxide is tungsten trioxide.7. The catalyst of claim 1 , wherein:81-87% by weight of the at least one fiber comprises the at least one zeolite; and1-19% by weight of the at least one fiber comprises the at least one metal oxide.8. The catalyst of claim 1 , wherein:the at least one fiber has a length in a range of 0.1-500 microns; andthe at least one fiber has a diameter in a range of 50-800 nanometers.9. The catalyst of claim 1 , wherein:the at least one fiber has a length-to-diameter aspect ratio in a range of 50:1 to 1,000:1.10. The catalyst of claim 1 , wherein:the hydrocracking catalyst is binder free.11. The catalyst of claim 1 , wherein:the at least one fiber comprises a plurality of fibers.12. The catalyst of claim 11 , wherein:the plurality of fibers form a fiber mat.13. A method of making a hydrocracking catalyst for petroleum hydrocracking claim 11 , comprising: ...

HYDROCRACKING CATALYSTS CONTAINING RARE EARTH CONTAINING POST-MODIFIED USY ZEOLITE, METHOD FOR PREPARING HYDROCRACKING CATALYSTS, AND METHOD FOR HYDROCRACKING HYDROCARBON OIL WITH HYDROCRACKING CATALYSTS

In accordance with one or more embodiments of the present disclosure, a catalyst composition includes a catalyst support and at least one hydrogenative component disposed on the catalyst support. The catalyst support includes at least one USY zeolite having a framework substituted with titanium and zirconium. The framework-substituted USY zeolite comprises at least one rare earth element. Methods of making and using such a catalyst in a hydrocracking process are also disclosed. 1. A catalyst composition comprising:a catalyst support comprising at least one framework-substituted ultra-stable Y-type (USY) zeolite substituted with zirconium atoms and titanium atoms, the at least one framework-substituted USY zeolite comprising at least one doped rare earth element; andat least one hydrogenative component disposed on the catalyst support.2. The catalyst composition of claim 1 , wherein the at least one framework-substituted USY zeolite is substituted with 0.1 wt. % to 5 wt. % zirconium atoms and 0.1 wt. % to 5 wt. % titanium calculated on an oxide basis.3. The catalyst composition of claim 1 , wherein the rare earth element is selected from the group consisting of scandium claim 1 , yttrium claim 1 , lanthanum claim 1 , cerium claim 1 , praseodymium claim 1 , neodymium claim 1 , promethium claim 1 , samarium claim 1 , europium claim 1 , gadolinium claim 1 , terbium claim 1 , dysprosium claim 1 , holmium claim 1 , erbium claim 1 , thulium claim 1 , ytterbium claim 1 , lutetium claim 1 , and a combination of two more thereof.4. The catalyst composition of claim 1 , wherein the framework-substituted USY zeolite comprises a crystal lattice constant from 2.43 nm to 2.45 nm.5. The catalyst composition of claim 1 , wherein the framework-substituted USY zeolite comprises a specific surface area from 600 m/g to 900 m/g.6. The catalyst composition of claim 1 , wherein the catalyst composition comprises a specific surface area from 200 m/g to 450 m/g.7. The catalyst composition of ...

Aromatic recovery complex with a hydrodearylation step to process clay tower effluents

The disclosure provides a process to hydrodearylate the non-condensed alkyl-bridged multi-aromatics at the outlet of the clay tower where such multi-aromatics form rather than performing hydrodearylation on the reject stream of the aromatics complex. Hydrodearylation may feature combining a C8+ hydrocarbon stream from a clay treater with a hydrogen stream over a catalyst bed comprising a support and an acidic component optionally containing Group 8 and/or Group 6 metals.

Coating for reducing nitrogen oxides

A catalyst coating for use in a hydrolysis catalyst (H-catalyst) for the reduction of nitrogen oxides, a manufacturing method for such a coating, a catalyst structure and its use are described. The H-catalyst includes alkaline compounds, which are capable of adsorbing HNCO and/or nitrogen oxides and which include alkali and alkaline earth metals, lanthanum and/or yttrium and/or hafnium and/or prasedium and/or gallium, and/or zirconium for promoting reduction, such as for promoting the hydrolysis of urea and the formation of ammonia and/or the selective reduction of nitrogen oxides.

Suspended-Bed Hydrogenation Catalyst and Regeneration Method Therefor

A suspended-bed hydrogenation catalyst and a regeneration method are disclosed. A composite support comprises a semi-coke pore-expanding material, a molecular sieve and a spent catalytic cracking catalyst. The hydrogenation catalyst for heavy oil is obtained through mixing the semi-coke pore-expanding material, the molecular sieve and the spent catalytic cracking catalyst, followed by molding, calcining and activating, and then loading an active metal oxide to the composite support. According to the composite support, a macropore, mesopore and micropore uniformly-distributed structure is formed, so that full contact between all ingredients in the heavy oil and active ingredients in a hydrogenation process is facilitated, and the conversion ratio of the heavy oil is increased. The hydrogenation catalyst integrates adsorption, cracking and hydrogenation properties. According to a regeneration method, the loading performance of an active-metal-loaded support in a spent hydrogenation catalyst cannot be destroyed. 1. A catalyst composite support , comprisinga semi-coke pore-expanding material,a molecular sieve anda spent catalytic cracking catalyst,wherein the mass ratio of the semi-coke pore-expanding material to the molecular sieve to the spent catalytic cracking catalyst is (1 to 5): (2 to 4): (0.5 to 5);{'sup': 2', '2, 'the semi-coke pore-expanding material has a specific surface area of 150 m/g to 300 m/g and an average pore size of 70 nm to 80 nm;'}{'sup': 2', '2, 'the molecular sieve has a specific surface area of 200 m/g to 300 m/g and an average pore size of 5 nm to 10 nm; and'}{'sup': 2', '2, 'the spent catalytic cracking catalyst has a specific surface area of 50 m/g to 300 m/g and an average pore size of 3 nm to 7 nm.'}2. The composite support according to claim 1 , wherein the semi-coke pore-expanding material has an average particle size of 60 to 100 microns and an average pore volume of 2 cm/g to 3 cm/g.3. The composite support according to claim 1 , ...

HYDROCRACKING CATALYST FOR HYDROCARBON OIL, METHOD FOR PRODUCING HYDROCRACKING CATALYST, AND METHOD FOR HYDROCRACKING HYDROCARBON OIL WITH HYDROCRACKING CATALYST

The present invention relates to a hydrocracking catalyst for hydrocarbon oil comprising a support containing a framework-substituted zeolite-1 in which zirconium atoms and/or hafnium atoms form a part of a framework of an ultrastable y-type zeolite and a hydrogenative metal component carried thereon and a method for producing the same. The hydrocracking catalyst of the present invention makes it easy to diffuse heavy hydrocarbon oils such as VGO, DAO and the like into mesopores, is improved in a cracking activity and makes it possible to obtain a middle distillate at a high yield as compared with catalysts prepared by using zeolite comprising titanium and/or zirconium carried thereon. 120-. (canceled)21. A hydrocracking catalyst for the high boiling fraction containing hydrocarbon oil comprising a hydrogenative metal component carried on a support containing an ultra-stable Y-type zeolite ,wherein the ultra-stable Y-type zeolite is a framework-substituted zeolite (hereinafter referred to as a framework-substituted zeolite-1) in which a part of aluminum atoms constituting a zeolite framework thereof is substituted with zirconium atoms and/or hafnium atoms,said zeolite-1 has a crystallinity of 80% or more, and contains from 0.1 to 5 mass % zirconium atoms and/or hafnium atoms as calculated as the oxide basis, anda relative decomposition rate as defined below is 99% or more, and a relative middle distillate yield as defined below is 95% or more:(Relative decomposition rate and relative middle distillate yield){'sup': −1', '3, 'claim-text': [{'br': None, 'Decomposition rate (%)={1−(Content (kg) of a fraction having a boiling point of higher than 375° C. in the produced oil/Content (kg) of a fraction having a boiling point of higher than 375° C. in the raw oil)}×100\u2003\u2003Equation (2), {'br': None, 'Middle distillate yield (%)={Content (kg) of a fraction having a boiling point of 149 to 375° C. in the produced oil/Content (kg) of a fraction having a boiling point ...

HYDRODESULFURIZATION CATALYST WITH A ZEOLITE-GRAPHENE MATERIAL COMPOSITE SUPPORT AND METHODS THEREOF

A hydrodesulfurization catalyst, which includes (i) a catalyst support including a zeolite doped with 0.1 to 0.5 wt. % of a graphene material, based on a total weight of the catalyst support, (ii) 5 to 20 wt. % of molybdenum, based on a total weight of the hydrodesulfurization catalyst, and (iii) 1 to 6 wt. % of a promoter selected from the group consisting of cobalt and nickel, based on a total weight of the hydrodesulfurization catalyst. The molybdenum and the promoter are homogeneously disposed on the catalyst support. A method of producing the hydrodesulfurization catalyst via incipient wetness impregnation techniques, and a method for desulfurizing a hydrocarbon feedstock with the hydrodesulfurization catalyst are also provided. 1: A hydrodesulfurization catalyst , comprising:a catalyst support comprising a zeolite doped with 0.1 to 0.5 wt. % of a graphene material, based on a total weight of the catalyst support;5 to 20 wt. % of molybdenum, based on a total weight of the hydrodesulfurization catalyst; and1 to 6 wt. % of a promoter selected from the group consisting of cobalt and nickel, based on a total weight of the hydrodesulfurization catalyst;wherein the molybdenum and the promoter are homogeneously disposed on the catalyst support.2: The hydrodesulfurization catalyst of claim 1 , wherein the zeolite is a Y-zeolite.3: The hydrodesulfurization catalyst of claim 1 , wherein the graphene material is present in the catalyst support in an amount of 0.3 to 0.4 wt. % claim 1 , based on a total weight of the catalyst support.4: The hydrodesulfurization catalyst of claim 1 , wherein the graphene material is graphene oxide.5: The hydrodesulfurization catalyst of claim 1 , wherein molybdenum is present in an amount of 14 to 16 wt. % claim 1 , and the promoter is present in an amount of 4 to 6 wt. % claim 1 , each based on a total weight of the hydrodesulfurization catalyst.6: The hydrodesulfurization catalyst of claim 1 , wherein the catalyst support consists of the ...

HYDROPROCESSING CATALYST AND HYDROPROCESSING CATALYST OF MAKING THE SAME

The present invention is directed to a hydroprocessing catalyst containing at least one catalyst support, one or more metals, optionally one or more molecular sieves, optionally one or more promoters, wherein deposition of at least one of the metals is achieved in the presence of a modifying agent. 1. A hydroprocessing catalyst , comprising:at least one molecular sieve which is a Y zeolite with a unit cell size of between 24.15 Å and 24.45 Å; and{'sub': '2', 'sup': 2', '2, 'at least one metal deposited on an amorphous silica-alumina catalyst support containing SiOin an amount of 10 wt. % to 70 wt. % of the dry bulk weight of the carrier as determined by ICP elemental analysis, a BET surface area of between 450 m/g and 550 m/g, a total pore volume of between 0.75 mL/g and 1.05 mL/g, and a mean mesopore diameter of between 70 Å and 130 Å;'}wherein deposition of the metal is achieved in the presence of a modifying agent and with the catalyst support after the deposition subjected to drying for a period of time ranging from 1 to 5 hours and at a temperature sufficient to remove impregnation solution solvent but below the decomposition temperature of the modifying agent.2. The hydroprocessing catalyst of claim 1 , wherein the Y zeolite has a silica-to-alumina ratio of greater than 10 claim 1 , a micropore volume of from 0.15 mL/g to 0.27 mL/g claim 1 , a BET surface area of from 700 m/g to 825 m/g claim 1 , and a unit cell size of from 24.15 Å to 24.45 Å.3. The hydroprocessing catalyst of claim 1 , wherein Y zeolite has a silica-to-alumina ratio of greater than 10 claim 1 , a micropore volume of from 0.15 mL/g to 0.27 mL/g claim 1 , a BET surface area of from 700 m/g to 825 m/g claim 1 , and a unit cell size of from 24.15 Å to 24.35 Å claim 1 , and a low-acidity claim 1 , highly dealuminated ultrastable Y zeolite having an Alpha value of less than about 5 and Brønsted acidity of from 1 to 40 micro-mole/g.5. The hydroprocessing catalyst of claim 1 , wherein the modifying ...

Novel catalysts and process for liquid hydrocarbon fuel production

The present invention provides a novel process and system in which a mixture of carbon monoxide and hydrogen synthesis gas, or syngas, is converted into hydrocarbon mixtures composed of high quality gasoline components, aromatic compounds, and lower molecular weight gaseous olefins in one reactor or step. The invention utilizes a novel molybdenum-zeolite catalyst in high pressure hydrogen for conversion, as well as a novel rhenium-zeolite catalyst in place of the molybdenum-zeolite catalyst, and provides for use of the novel catalysts in the process and system of the invention. 1. A process for the production of hydrocarbon fuel products having an aromatic content of about 90% or greater from synthesis gas comprising:providing a synthesis gas; andproviding an alcohol-forming catalyst;providing a single reaction system and steam reformer in which the chemical reactions occur over the alcohol-forming catalyst found in the same matrix as a gasoline-forming catalyst, with the synthesis gas contacted in a Fischer-Tropsch reaction with the alcohol-forming catalyst in high pressure hydrogen;wherein the alcohol-forming catalyst is a zeolite-encaged, molybdenum-based catalyst active for deoxy-aromatization of alcohols and synthesis gas to mixed alcohols, isomerization of alkanes, and aromatization; andwherein the alcohol-forming catalyst produces high quality alcohols from the synthesis gas.2. The process of claim 1 , wherein the catalyst is a cluster comprising a molybdenum oxide represented by MoCOencaged in a zeolite and wherein the cluster comprises the active phase.3. The process of claim 2 , wherein the cluster comprises a molybdenum sulfide.4. The process of claim 3 , wherein the cluster further comprises at least one metal modifier selected from the group consisting of the elements of Groups 1A and 2A of the Periodic Table and mixtures of the aforementioned elements.5. The process of claim 3 , wherein the zeolite comprises a support claim 3 , and comprises one or ...

Middle distillate hydrocracking catalyst

The present invention is directed to an improved hydrocracking catalyst containing an amorphous silica-alumina (ASA) base and alumina support. The ASA base is characterized as having a high nanopore volume and low particle density. The alumina support is characterized as having a high nanopore volume. Hydrocracking catalysts employing the combination high nanopore volume ASA base and alumina support exhibit improved hydrogen efficiency, and greater product yield and quality, as compared to hydrocracking catalysts containing conventional ASA base and alumina components.

Catalysts, systems, and processes for regulating a contacting state in producing light olefins from paraffins

The present invention relates to catalysts, catalyst systems, and processes for the production of valuable light olefins, such as ethylene, from paraffinic hydrocarbons, such as propane, through dehydrogenation and metathesis. The contacting state between dehydrogenation and metathesis catalysts can advantageously be manipulated using an inert or relatively inert coating or outer shell that provides a degree of physical separation between catalytically active centers or inner cores. This has been discovered to significantly increase olefin selectivity (i.e., reduce undesired hydrogenation/hydrogenolysis side reactions) without an appreciable paraffin conversion deficit, such that the overall yield of desired olefinic hydrocarbons such as ethylene is thereby significantly increased.

BIMETAL CATALYSTS

The present disclosure discloses bimetal catalysts. 1. A catalyst , comprising:a carbide or nitride of two early transition metals, and{'sup': 2', '−1, 'a mesoporous support having a surface area of at least about 170 mg, the carbide or nitride of the two early transition metals being supported by the mesoporous support and in an amorphous form.'}2. The catalyst of claim 1 , wherein the support in the presence of the carbide or nitride has a surface area of at least about 450 mg.3. The catalyst of claim 1 , wherein the support in the presence of the carbide or nitride has a surface area of at least about 700 mg.4. The catalyst of claim 1 , wherein the support in the presence of the carbide or nitride has a pore volume of at least about 0.1 cmg.5. The catalyst of claim 1 , wherein the support in the presence of the carbide or nitride has a pore volume of at least about 0.2 cmg.6. The catalyst of claim 1 , wherein the support in the presence of the carbide or nitride has a pore volume of at least about 0.7 cmg.7. The catalyst of claim 1 , wherein one of the two early transition metals is Mo claim 1 , W claim 1 , Co claim 1 , Fe claim 1 , Rh or Mn.8. The catalyst of claim 1 , wherein one of the two early transition metals is Mo.9. The catalyst of claim 1 , wherein one of the two early transition metals is W.10. The catalyst of claim 7 , wherein the other early transition metal is Ni claim 7 , Co claim 7 , Al claim 7 , Si claim 7 , S or P.11. The catalyst of claim 7 , wherein the other early transition metal is Ni.12. The catalyst of claim 7 , wherein the other early transition metal is Co.13. The catalyst of claim 1 , wherein the support is selected from the group consisting of AlO claim 1 , SiO claim 1 , a zeolite claim 1 , ZrO claim 1 , CeO claim 1 , a mesoporous material claim 1 , a clay claim 1 , and combinations thereof.14. The catalyst of claim 13 , wherein the support is selected from the group consisting of ZSM-5 claim 13 , zeolite β claim 13 , USY claim 13 , ...

Middle distillate hydrocracking catalyst containing zeolite usy, and zeolite beta with low acidity and large domain size

A hydrocracking catalyst is provided comprising: a zeolite beta having an OD acidity of 20 to 50 μmol/g and an average crystal size from 300 to 800 nanometers; a zeolite USY; wherein a wt % of the zeolite beta is less than the wt % of the zeolite USY; a support comprising an amorphous silica aluminate and a second support material; and at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table. A process for hydrocracking a hydrocarbonaceous feedstock is provided, comprising: contacting the hydrocarbonaceous feedstock with the hydrocracking catalyst under hydrocracking conditions to produce a hydrocracked effluent that comprises middle distillates. A method for making the hydrocracking catalyst is also provided.

CRACKING CATALYST COMPRISING PLATINUM ENCAPSULATED IN MICROPOROUS SILICA

According to the subject matter of the present disclosure, a cracking catalyst may comprise zeolite, alumina, nickel oxide, hydrogenation metal, and a core shell Pt/SiO. The core shell Pt/SiOmay comprise a platinum nanoparticle encapsulated by a microporous SiOlayer. 1. A cracking catalyst comprising zeolite , alumina , nickel oxide , a hydrogenation metal , and a core shell Pt/SiO , wherein the core shell Pt/SiOcomprises a platinum nanoparticle encapsulated by a microporous SiOlayer.2. The cracking catalyst of claim 2 , wherein an average pore size of the microporous SiOlayer is from 0.25 nm to 1.5 nm.3. The cracking catalyst of claim 2 , wherein a maximum pore size of the microporous SiOlayer is 1.5 nm.4. The cracking catalyst of claim 1 , wherein the microporous SiOlayer has an average thickness of 6 nm to 10 nm.5. The cracking catalyst of claim 4 , wherein the microporous SiOlayer has a maximum thickness and a minimum thickness claim 4 , the maximum thickness is less than 4 nm greater than the minimum thickness.6. The cracking catalyst of claim 1 , wherein the Pt nanoparticle is from 0.5 nm to 6 nm in diameter.7. The cracking catalyst of claim 1 , wherein the hydrogenation metal is one or both of MoOand WO.8. The cracking catalyst of claim 1 , wherein the hydrogenation metal comprises WOand the catalyst comprises from 20 wt. % to 26 wt. % WO claim 1 , from 4 wt. % to 6 wt. % NiO claim 1 , from 10 wt. % to 60 wt. % zeolite claim 1 , from 1 wt. % to 10 wt. % core shell Pt/SiO claim 1 , and from 10 wt. % to 60 wt. % alumina.9. The cracking catalyst of claim 1 , wherein the hydrogenation metal comprises MoOand the catalyst comprises from 14 wt. % to 16 wt. % MoO claim 1 , from 4 wt. % to 6 wt. % NiO claim 1 , from 10 wt. % to 50 wt. % zeolite claim 1 , from 1 wt. % to 10 wt. % core shell Pt/Sift claim 1 , and from 20 wt. % to 70 wt. % alumina.10. The cracking catalyst of claim 1 , wherein the zeolite comprises ultra-stable zeolite Y (USY).11. A method of using the ...

Method of Forming a Catalyst with an Ion-Modified Binder

An alkylation catalyst having a zeolite catalyst component and a binder component providing mechanical support for the zeolite catalyst component is disclosed. The binder component is an ion-modified binder that can include metal ions selected from the group consisting of Co, Mn, Ti, Zr, V, Nb, K, Cs, Ga, B, P, Rb, Ag, Na, Cu, Mg, Fe, Mo, Ce, and combinations thereof The metal ions reduce the number of acid sites on the zeolite catalyst component. The metal ions can range from 0.1 to 50 wt % based on the total weight of the ion-modified binder. Optionally, the ion-modified binder is present in amounts ranging from 1 to 80 wt % based on the total weight of the catalyst.

HYDROCRACKING CATALYST FOR HYDROCARBON OIL, METHOD FOR PRODUCING HYDROCRACKING CATALYST, AND METHOD FOR HYDROCRACKING HYDROCARBON OIL WITH HYDROCRACKING CATALYST

The present invention relates to a hydrocracking catalyst for hydrocarbon oil comprising a support containing a framework-substituted zeolite-1 in which zirconium atoms and/or hafnium atoms form a part of a framework of an ultrastable y-type zeolite and a hydrogenative metal component carried thereon and a method for producing the same. The hydrocracking catalyst of the present invention makes it easy to diffuse heavy hydrocarbon oils such as VGO, DAO and the like into mesopores, is improved in a cracking activity and makes it possible to obtain a middle distillate at a high yield as compared with catalysts prepared by using zeolite comprising titanium and/or zirconium carried thereon. 1. A hydrocracking catalyst for hydrocarbon oil comprising a hydrogenative metal component carried on a support containing an ultra-stable Y-type zeolite , wherein the above ultra-stable Y-type zeolite is a framework-substituted zeolite (hereinafter referred to as a framework-substituted zeolite-1) in which a part of aluminum atoms constituting a zeolite framework thereof is substituted with zirconium atoms and/or hafnium atoms.2. A hydrocracking catalyst for hydrocarbon oil according to claim 1 , wherein said zeolite-1 contains from 0.1 to 5 mass % zirconium atoms and/or hafnium atoms as calculated as the oxide basis.3. The hydrocracking catalyst for hydrocarbon oil according to or claim 1 , wherein said zeolite-1 further contains titanium atoms.4. The hydrocracking catalyst for hydrocarbon oil according to claim 3 , wherein in the zeolite-1 claim 3 , a part of the aluminum atoms forming the zeolite framework is further substituted with titanium atoms.5. The hydrocracking catalyst for hydrocarbon oil according to or claim 3 , wherein said zeolite-1 contains from 0.1 to 5 mass % titanium atoms as calculated as the oxide basis.65. The hydrocracking catalyst for hydrocarbon oil according to any of to claims 1 , wherein the support contains the zeolite-1 and inorganic oxide excluding 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 ...

HYDROCRACKING CATALYST

Process for preparing a hydrocracking catalyst carrier which process comprises subjecting a carrier comprising an amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10 to calcination at a temperature of from 700 to 900° C., hydrocracking catalyst carrier comprising amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10, the infrared spectrum of which catalyst has a peak at 3690 cm, substantially reduced peaks at 3630 cmand 3565 cmand no peak at 3600 cm, hydrocracking catalyst carrier comprising an amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10, which catalyst has an acidity as measured by exchange with perdeuterated benzene of at most 20 micromole/gram, hydrocracking catalyst derived from such carrier and hydrocracking process with the help of such catalyst. 1. A hydrocracking catalyst carrier obtainable by a preparation process comprising: calcining zeolite Y , having a silica to alumina molar ratio of at least 10 , in the absence of added steam at a temperature in the range of from 700° C. to 1000° C. followed by mixing the obtained zeolite Y with an amorphous binder , comprising silica-alumina containing silica in an amount in the range of from 25 to 95% by weight as calculated on the carrier alone , and an acidic aqueous solution in amount so as to provide a mixture having a pH in the range of from 4.4 to 5.7 and an LOI in the range of from 50 to 65% such that said hydrocracking catalyst carrier has a monomodal pore size distribution , wherein at least 50% of the total pore volume is present in pores having a diameter in the range of from 4 to 50 nm; extruding said mixture to give an extrudate; and calcining said extrudate at a temperature of from 700 to 1000° C.2. A hydrocracking catalyst carrier which comprises amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10 , the infrared spectrum of which carrier has a peak at 3690 cm , ...

Novel catalysts and process for liquid hydrocarbon fuel production

The present invention provides a novel process and system in which a mixture of carbon monoxide and hydrogen synthesis gas, or syngas, is converted into hydrocarbon mixtures composed of high quality gasoline components, aromatic compounds, and lower molecular weight gaseous olefins in one reactor or step. The invention utilizes a novel molybdenum-zeolite catalyst in high pressure hydrogen for conversion, as well as a novel rhenium-zeolite catalyst in place of the molybdenum-zeolite catalyst, and provides for use of the novel catalysts in the process and system of the invention. 1. A process for the production of hydrocarbon fuel products having an aromatic content of about 90% or greater from synthesis gas comprising:providing a synthesis gas; andproviding an alcohol-forming catalyst;providing a single reaction system and steam reformer in which the chemical reactions occur over the alcohol-forming catalyst found in the same matrix as a gasoline-forming catalyst, with the synthesis gas contacted in a Fischer-Tropsch reaction with the alcohol-forming catalyst in high pressure hydrogen;wherein the alcohol-forming catalyst is a zeolite-encaged, molybdenum-based catalyst active for deoxy-aromatization of alcohols and synthesis gas to mixed alcohols, isomerization of alkanes, and aromatization; andwherein the alcohol-forming catalyst produces high quality alcohols from the synthesis gas.2. The process of claim 1 ,wherein the catalyst is a cluster comprising a molybdenum oxide represented by MoCOencaged in a zeolite and wherein the cluster comprises the active phase.3. The process of claim 2 , wherein the cluster comprises a molybdenum sulfide.4. The process of claim 3 , wherein the cluster further comprises at least one metal modifier selected from the group consisting of the elements of Groups 1A and 2A of the Periodic Table and mixtures of the aforementioned elements.5. The process of claim 3 , wherein the zeolite comprises a support claim 3 , and comprises one or more ...

HYDROCARBON CONVERSION CATALYST

The present invention relates to a hydrocarbon conversion catalyst, comprising: a first composition comprising a dehydrogenation active metal on a solid support, and a second composition comprising a transition metal and a doping agent, wherein the doping agent is selected from zinc, gallium, indium, lanthanum, and mixtures thereof, on an inorganic support. 1. A hydrocarbon conversion catalyst , comprising:a first composition comprising a dehydrogenation active metal on a solid support; anda second composition comprising a transition metal and a doping agent on an inorganic support, wherein the doping agent is selected from zinc, gallium, indium, lanthanum, and mixtures thereof.2. The hydrocarbon conversion catalyst according to claim 1 , wherein the dehydrogenation active metal is selected from platinum claim 1 , palladium claim 1 , iridium claim 1 , chromium claim 1 , and mixtures thereof.3. The hydrocarbon conversion catalyst according to claim 1 , wherein the solid support is selected from aluminum oxide claim 1 , silicon dioxide claim 1 , zirconium dioxide claim 1 , titanium dioxide claim 1 , magnesium oxide claim 1 , calcium oxide claim 1 , and mixtures thereof.4. The hydrocarbon conversion catalyst according to claim 1 , wherein the first composition further comprises an additional active metal selected from potassium claim 1 , tin claim 1 , lanthanum claim 1 , indium claim 1 , yttrium claim 1 , ytterbium claim 1 , rhenium claim 1 , and mixtures thereof.5. The hydrocarbon conversion catalyst according to claim 1 , wherein the first composition contains 0.01 to 25 wt % of the dehydrogenation active metal based on the total weight of the first composition.6. The hydrocarbon conversion catalyst according to claim 1 , wherein the first composition contains 0.005 to 2 wt % of the additional active metal based on the total weight of the first composition.7. The hydrocarbon conversion catalyst according to claim 1 , wherein the transition metal is selected from ...

INORGANIC POROUS FRAMEWORK-LAYERED DOUBLE HYDROXIDE CORE-SHELL MATERIALS AS CATALYST SUPPORTS IN ETHYLENE POLYMERISATION

A catalyst system comprises an activated solid support material and having, on its surface, one or more catalytic transition metal complexes. 1. A catalyst system comprising an activated solid support material and having , on its surface , one or more catalytic transition metal complex , wherein the solid support material comprises a core@layered double hydroxide shell material having the formula I{'br': None, 'sub': p', '(1−x)', 'x', '2', 'a/n', '2', 'q, 'sup': z+', 'y+', 'a+', 'n−, 'T@ {[MM′(OH)](X).bHO.c(AMO-solvent)}\u2003\u2003(I)'}wherein T is a solid, porous, inorganic oxide-containing framework material,{'sup': z+', 'y+', 'z+, 'M and M are independently selected charged metal cations; M is a metal cation of charge z or a mixture of two or more metal cations each independently having the charge z;'}{'sup': 'y+', 'M′ is a metal cation of charge y or a mixture of two or more metal cations each independently having the charge y;'}z=1 or 2;y=3 or 4;00;q>0;{'sup': 'n−', 'X is an anion; with n>0;'}a=z(1−x)+xy−2; andAMO-solvent is an organic solvent which is completely miscible with water.2. The catalyst system according to claim 1 , wherein M′ is Al claim 1 , and/or M is Li claim 1 , Mg or Ca and/or X is selected from CO claim 1 , OH claim 1 , F claim 1 , Cl claim 1 , Br claim 1 , I claim 1 , SO claim 1 , NO and PO claim 1 , preferably CO claim 1 , Cl and NO claim 1 , or mixtures thereof.3. The catalyst system according to claim 1 , wherein the AMO-solvent is selected from acetone claim 1 , methanol claim 1 , ethanol or isopropanol claim 1 , preferably acetone or ethanol.4. The catalyst system according to claim 1 , wherein T is a molecular sieve material selected from silicate claim 1 , aluminium silicate claim 1 , vanadium silicate claim 1 , iron silicate claim 1 , silicon-aluminium phosphate (SAPO) and aluminium phosphate (AIPO).5. The catalyst system according to claim 1 , wherein T is an aluminium silicate having a silicon ...

Catalyst for removal of sulphur oxides from flue gases of power plants

The present invention relates to the catalytic processes for rendering harmless the flue gases of the power stations or more precisely to the catalysts for sulfur oxides reduction to elemental sulfur. The novel catalyst presents the binary polycations of copper and zinc or copper and manganese incorporated into the low silica faujasite X (LSX) having transition metals ratio Cu:Zn or Cu:Mn in the range of 2:1 to 4:1.

MIDDLE DISTILLATE HYDROCRACKING CATALYST CONTAINING HIGHLY NANOPOROUS STABILIZED Y ZEOLITE

Described herein is an improved hydrocracking catalyst containing a high nanopore volume (HNPV) stabilized Y (SY) zeolite. The HNPV SY zeolite is also characterized as having an enhanced acid site distribution as compared to conventional SY zeolites. 1. A hydrocracking catalyst , comprising:a support;an amorphous silica alumina material;a high nanopore volume stabilized Y zeolite having a nanopore volume in the 20 nm to 50 nm range of 0.15 to 0.6 cc/g; andat least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table.2. The hydrocracking catalyst of claim 1 , wherein the high nanopore volume stabilized Y zeolite has an acid site distribution index factor of between 0.02 and 0.12.3. The hydrocracking catalyst of claim 2 , wherein high nanopore volume stabilized Y zeolite has an acid site distribution index factor of between 0.06 and 0.12.4. The hydrocracking catalyst of claim 2 , wherein high nanopore volume stabilized Y zeolite has an acid site distribution index factor of between 0.08 and 0.11.5. The hydrocracking catalyst of claim 1 , wherein 20 to 30% of the nanopores are in the 8 nm to 20 nm range.6. The hydrocracking catalyst of claim 1 , wherein 40 to 60% of the nanopores are in the 20 nm to 50 nm range.7. The hydrocracking catalyst of claim 1 , wherein 15 to 25% of the nanopores are greater than 50 nm.8. A process for hydrocracking a hydrocarbonaceous feedstock claim 1 , comprising contacting the feedstock with a hydrocracking catalyst under hydrocracking conditions to produce a hydrocracked effluent; a support;', 'an amorphous silica alumina material;', 'a high nanopore volume stabilized Y zeolite having a nanopore volume in the 20 nm to 50 nm range of 0.15 to 0.6 cc/g; and', 'at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table., 'the hydrocracking catalyst comprising'}9. The process of claim 8 , wherein the high nanopore ...

MIDDLE DISTILLATE HYDROCRACKING CATALYST CONTAINING HIGHLY A STABILIZED Y ZEOLITE WITH ENHANCED ACID SITE DISTRIBUTION

Described herein is an improved hydrocracking catalyst containing a stabilized Y zeolite (SY) having an enhanced acid site distribution as compared to conventional SY zeolites. The SY zeolite is also characterized as having a high nanopore volume (HNPV). 1. A hydrocracking catalyst , comprising:a support;an amorphous silica alumina material;a stabilized Y zeolite having an acid site distribution index factor of between 0.02 and 0.12; andat least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table.2. The hydrocracking catalyst of claim 1 , wherein the stabilized Y zeolite is a high nanopore volume stabilized Y zeolite having a nanopore volume in the 20 nm to 50 nm range of 0.15 to 0.6 cc/g.3. The hydrocracking catalyst of claim 2 , wherein 20 to 30% of the nanopores are in the 8 nm to 20 nm range.4. The hydrocracking catalyst of claim 2 , wherein 40 to 60% of the nanopores are in the 20 nm to 50 nm range.5. The hydrocracking catalyst of claim 2 , wherein 15 to 25% of the nanopores are greater than 50 nm.6. The hydrocracking catalyst of claim 1 , wherein high nanopore volume stabilized Y zeolite has an acid site distribution index factor of between 0.06 and 0.12.4. The hydrocracking catalyst of claim 1 , wherein high nanopore volume stabilized Y zeolite has an acid site distribution index factor of between 0.08 and 0.11.8. A process for hydrocracking a hydrocarbonaceous feedstock claim 1 , comprising contacting the feedstock with a hydrocracking catalyst under hydrocracking conditions to produce a hydrocracked effluent; a support;', 'an amorphous silica alumina material;', 'a stabilized Y zeolite having an acid site distribution index factor of between 0.02 and 0.12; and', 'at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table., 'the hydrocracking catalyst comprising'}9. The process of claim 8 , wherein the stabilized Y zeolite is a ...

HYDROCRACKING CATALYST, PREPARATION METHOD AND USE THEREOF, AND METHOD FOR HYDROCRACKING CATALYTIC DIESEL OIL

The present disclosure provides a hydrocracking catalyst, a method for preparing the same and a use of the same, and a method for hydrocracking catalytic diesel oil. The catalyst comprises a support, an active metal component, and carbon, wherein, based on the total weight of the catalyst, the content of the support is 60 to 90 wt %, the content of the active metal component calculated in metal oxides is 15 to 40 wt %, and the content of carbon calculated in C element is 1 to 5 wt %; measured with an infrared acidimetric estimation method, the acid properties of the hydrocracking catalyst are: the total infrared acid amount is 0.4 to 0.8 mmol/g, wherein, the infrared acid amount of strong acid with desorption temperature greater than 350° C. is 0.08 mmol/g or lower, and the ratio of the total infrared acid amount to the infrared acid amount of strong acid with desorption temperature greater than 350° C. is 5 to 50. 1. A hydrocracking catalyst , comprising a support , an active metal component , and carbon , wherein , based on the total weight of the catalyst , the content of the support is 60 to 90 wt % , the content of the active metal component calculated in metal oxides is 15 to 40 wt % , and the content of carbon calculated in C element is 1 to 5 wt %; measured with an infrared acidimetric estimation method , the acid properties of the hydrocracking catalyst are: the total infrared acid amount is 0.4 to 0.8 mmol/g , wherein , the infrared acid amount of strong acid with desorption temperature greater than 350° C. is 0.08 mmol/g or lower , and the ratio of the total infrared acid amount to the infrared acid amount of strong acid with desorption temperature greater than 350° C. is 5 to 50.2. The catalyst according to claim 1 , wherein claim 1 , the support is a silica-alumina support that contains a modified Y-type molecular sieve claim 1 , and claim 1 , based on the total weight of the support claim 1 , the support contains 20 to 85 wt % modified Y-type molecular ...

HYDROCRACKING CATALYST AND PROCESS FOR PRODUCING LUBE BASE STOCKS

Hydrocracking catalysts and hydrocracking processes for the selective production of lube base stocks are disclosed. The hydrocracking catalyst contains a low acidity, highly dealuminated USY zeolite having a zeolite acid site density of from 1 to 100 micromole/g, a catalyst support, and one or more metals. The hydrocracking catalysts can maximize lube base stock yield while providing for effective impurity removal and VI enhancement at lower hydrocracking conversions. 1. A hydrocracking catalyst , comprising: (a) a USY zeolite component having a SiO/AlOmole ratio of at least 50 , an alpha value of not more than 5 , and a zeolite acid site density of from 1 to 100 micromole/g; (b) an amorphous cracking component; and (c) at least one hydrogenation metal component selected from the group consisting of a Group VIB metal , a Group VIII metal , and mixtures thereof.2. The catalyst of claim 1 , wherein the zeolite component has a SiO/AlOmole ratio of from 80 to 150.3. The catalyst of claim 1 , wherein the zeolite component has an alpha value of from 0.01 to 3.4. The catalyst of claim 1 , wherein the zeolite component has a zeolite acid site density of from 1 to 50 micromole/g.5. The catalyst of claim 1 , wherein the hydrocracking catalyst has a residual zeolite micropore volume of at least 50%.6. The catalyst of claim 1 , wherein the hydrocracking catalyst has a residual zeolite micropore volume of at least 80%.7. The catalyst of claim 1 , wherein the amorphous cracking component is a silica-alumina containing SiOin an amount of from 10 to 70 wt. % of the bulk dry weight of the carrier as determined by ICP elemental analysis and having a mean mesopore diameter of from 7 to 13 nm claim 1 , a BET surface area of from 450 to 550 m/g claim 1 , and a total pore volume of from 0.57 to 1.05 mL/g.8. The catalyst of claim 1 , wherein the hydrogenation metal component is selected from the group consisting of molybdenum claim 1 , tungsten claim 1 , nickel claim 1 , cobalt claim 1 , ...

Na-Y Molecular Sieve, H-Y Molecular Sieve, and Preparation Methods Thereof, Hydrocracking Catalyst, and Hydrocracking Method

Provided is a Na—Y molecular sieve and a method for preparing the Na—Y molecular sieve, an H—Y molecular sieve and a method for preparing the H—Y molecular sieve, a hydrocracking catalyst, and a hydrocracking method. The average grain diameter of the Na—Y molecular sieve is 2-5 μm, and the sum of pore volumes of pores in 1-10 nm diameter accounts for 70-90% of the total pore volume of the Na—Y molecular sieve. The H—Y molecular sieve obtained from the large-grain Na—Y molecular sieve can be used as an acidic component in the hydrocracking catalyst. When the hydrocracking catalyst containing the H—Y molecular sieve is applied in the hydrocracking reaction of heavy oils that contain macromolecules, it can provide better cracking activity and product selectivity in the hydrocracking reaction.

MESOPOROUS COMPOSITE OF MOLECULAR SIEVES FOR HYDROCRACKING OF HEAVY CRUDE OILS AND RESIDUES

A hydrocracking catalyst having a support of a composite of mesoporous materials, molecular sieves and alumina, is used in the last bed of a multi-bed system for treating heavy crude oils and residues and is designed to increase the production of intermediate distillates having boiling points in a temperature range of 204° C. to 538° C., decrease the production of the heavy fraction (>538° C.), and increase the production of gasoline fraction (<204° C.). The feedstock to be processed in the last bed contains low amounts of metals and is lighter than the feedstock that is fed to the first catalytic bed. 1. A method for treating heavy crude oils and residues comprising the steps of;{'sup': 2', '3, 'feeding the heavy crude oil feedstock containing residues to a hydrocracking reaction zone of a reactor in the presence of a catalyst support obtained from boehmite, zeolite Y, and SBA-15 in a molar ratio of 60-85:5-15:10-35, respectively, and where said catalyst has a cylindrical shape and includes 3-15 wt % of a Group. VIB metal comprising molybdenum as molybdenum oxide or molybdenum sulfide and 1-5wt % of a Group VIII metal comprising nickel as nickel oxide or nickel sulfide, said catalyst having a specific surface area of 150-300 m/g, an average pore diameter of 6.0 to 15.0 nm, a pore volume of 0.2 to 0.7 cm/g, and a pore distribution of 20% of pores having a diameter of up to 5 nm, 70 to 85% of pores having a diameter of 5 to 50 run, and less than 5% of pores having a diameter greater than 50 nm, and a total acidity at 100° C. equivalent to 180 to 360 micromoles of pyridine per gram of catalyst; and'}hydrocracking the heavy crude oil feedstock in the presence of said catalyst to obtain a reaction product.2. The method of claim 1 , wherein said reaction product has an increased API gravity with respect to said heavy crude oil feedstock.3. The method of claim 1 , wherein said catalyst has a cylindrical shape with a diameter of 1.59 mm and a length of 2-7 mm.4. The method ...

HYDROCRACKING CATALYST AND PROCESS FOR PRODUCING LUBE BASE STOCKS

Hydrocracking catalysts and hydrocracking processes for the selective production of lube base stocks are disclosed. The hydrocracking catalyst contains a low acidity, highly dealuminated USY zeolite having a zeolite acid site density of from 1 to 100 micromole/g, a catalyst support, and one or more metals. The hydrocracking catalysts can maximize lube base stock yield while providing for effective impurity removal and VI enhancement at lower hydrocracking conversions. 1. A hydrocracking catalyst , comprising: (a) a USY zeolite component having a SiO/AlOmole ratio of at least 50 , an alpha value of not more than 5 , and a zeolite acid site density of from 1 to 100 micromole/g; (b) an amorphous cracking component; and (c) at least one hydrogenation metal component selected from the group consisting of a Group VIB metal , a Group VIII metal , and mixtures thereof.2. The catalyst of claim 1 , wherein the zeolite component has a SiO/AlOmole ratio of from 80 to 150.3. The catalyst of claim 1 , wherein the zeolite component has an alpha value of from 0.01 to 3.4. The catalyst of claim 1 , wherein the zeolite component has a zeolite acid site density of from 1 to 50 micromole/g.5. The catalyst of claim 1 , wherein the hydrocracking catalyst has a residual zeolite micropore volume of at least 50%.6. The catalyst of claim 1 , wherein the hydrocracking catalyst has a residual zeolite micropore volume of at least 80%.7. The catalyst of claim 1 , wherein the amorphous cracking component is a silica-alumina containing SiOin an amount of from 10 to 70 wt. % of the bulk dry weight of the carrier as determined by ICP elemental analysis and having a mean mesopore diameter of from 7 to 13 nm claim 1 , a BET surface area of from 450 to 550 m/g claim 1 , and a total pore volume of from 0.57 to 1.05 mL/g.8. The catalyst of claim 1 , wherein the hydrogenation metal component is selected from the group consisting of molybdenum claim 1 , tungsten claim 1 , nickel claim 1 , cobalt claim 1 , ...

Process for preparing a mesoporized catalyst, catalyst thus obtained and use thereof in a catalytic process

The invention relates to a process for preparing a catalyst comprising a mesoporized zeolite, comprising the steps of: preparation of a protonic mesoporized zeolite, which contains at least one network of micropores and at least one network of mesopores, and treatment in a gas or liquid phase containing ammonia or ammonium ions. The invention also related to the obtained catalyst and the use of this catalyst in hydroconversion processes.

ADDITIVES FOR GAS PHASE OXIDATIVES DESULFURIZATION CATALYSTS

A composition useful in oxidative desulphurization of gaseous hydrocarbons is described. It comprises a CuZnAl—O mixed oxide, and an H form of a zeolite. The mixed oxide can contain one or more metal oxide promoters. The H form of the zeolite can be desilicated, and can also contain one or more transition metals. 1. A composition useful in oxidative desulfurization of gaseous , sulfur containing hydrocarbons , (i) a CuZnAl—O mixed oxide component comprising nominal copper oxide in an amount ranging from 10 weight percent (wt %) to 50 wt % , zinc oxide in an amount ranging from 5 wt % to less than 20 wt % , and aluminum oxide in an amount ranging from 20 wt % to 70 wt % , wherein said catalytic composition has a highly dispersed spinel oxide phase with a formula CuZnAlOwherein x ranges from 0 to 1 , dispersed crystalline ZnO and CaO , and (ii) at least one zeolite in , desilicated H form.2. The composition of claim 1 , wherein said CuZnAl—O mixed oxide component is in granular form.3. The composition of claim 2 , formed as a cylinder claim 2 , a sphere claim 2 , a trilobe claim 2 , or a quatrolobe.4. The composition of claim 2 , wherein granules of said CuZnAl—O mixed oxide component have a diameter of from 1 mm to 4 mm.5. The composition of claim 1 , wherein said CuZnAl—O mixed oxide component has a surface area of from 10 m/g to 100 m/g.6. The composition of claim 1 , wherein the total pore volume of said CuZnAl—O mixed oxide component is from about 0.1 cm/g to about 0.5 cm/g.7. The composition of claim 1 , said CuZnAl—O mixed oxide component comprises from 20 wt % to 45 wt % CuO claim 1 , from 10 wt % to less than 20 wt % ZnO claim 1 , and from 20 wt % to 70 wt % of AlO.8. The composition of claim 7 , said CuZnAl—O mixed oxide component comprising from 30 wt % to 45 wt % CuO claim 7 , from 12 wt % to less than 20 wt % ZnO claim 7 , and from 20 wt % to 40 wt % AlO.9. The composition of claim 5 , said CuZnAl—O mixed oxide component having a surface area of from 50 m ...

Na-Y Molecular Sieve, H-Y Molecular Sieve, and Preparation Methods Thereof, Hydrocracking Catalyst, and Hydrocracking Method

Provided is a Na—Y molecular sieve and a method for preparing the Na—Y molecular sieve, an H—Y molecular sieve and a method for preparing the H—Y molecular sieve, a hydrocracking catalyst, and a hydrocracking method. The average grain diameter of the Na—Y molecular sieve is 2-5 μm, and the sum of pore volumes of pores in 1-10 nm diameter accounts for 70-90% of the total pore volume of the Na—Y molecular sieve. The H—Y molecular sieve obtained from the large-grain Na—Y molecular sieve can be used as an acidic component in the hydrocracking catalyst. When the hydrocracking catalyst containing the H—Y molecular sieve is applied in the hydrocracking reaction of heavy oils that contain macromolecules, it can provide better cracking activity and product selectivity in the hydrocracking reaction. 1. A hydrocracking catalyst , wherein the support in the catalyst contains an H—Y molecular sieve , wherein the crystal cell parameter of the H—Y molecular sieve is 2.425-2.450 nm; the mole ratio of SiO/AlOin the H—Y molecular sieve is 10-120:1; the sum of pore volumes of pores in 2-7 nm diameter in the H—Y molecular sieve is 60-95% of the total pore volume; the specific surface area of the H—Y molecular sieve is 750-980 m/g; and , the total acid amount measured by near infrared spectroscopy in the H—Y molecular sieve is 0.1-1.0 mmol/g.2. The hydrocracking catalyst according to claim 1 , wherein the crystal cell parameter of the H—Y molecular sieve is 2.436-2.450 nm; the mole ratio of SiO/AlOin the H—Y molecular sieve is 10-50:1; the sum of pore volumes of pores in 2-6 nm diameter in the H—Y molecular sieve is 60-90% of the total pore volume; the specific surface area of the H—Y molecular sieve is 750-950 m/g; and claim 1 , the total acid amount measured by near infrared spectroscopy in the H—Y molecular sieve is 0.5-1.0 mmol/g.3. The hydrocracking catalyst according to claim 1 , wherein the crystal cell parameter of the H—Y molecular sieve is 2.425-2.435 nm; the mole ratio of SiO ...

ZEOLITIC CATALYTIC CONVERSION OF ALCOHOLS TO HYDROCARBONS

A method for converting an alcohol to a hydrocarbon, the method comprising contacting said alcohol with a metal-loaded zeolite catalyst at a temperature of at least 100° C. and up to 550° C., wherein said alcohol can be produced by a fermentation process, said metal is a positively-charged metal ion, and said metal-loaded zeolite catalyst is catalytically active for converting said alcohol to said hydrocarbon. 1. A method for converting ethanol to an aromatic hydrocarbon , the method comprising contacting said ethanol with a metal-loaded zeolite catalyst at a temperature of at least 300° C. and up to 550° C. , said metal is a positively-charged metal ion , and said metal-loaded zeolite catalyst is catalytically active for converting said ethanol to said hydrocarbon.2. (canceled)3. The method of claim 1 , wherein said ethanol is a component of an aqueous solution.4. The method of claim 1 , wherein said ethanol is a component of an aqueous solution in a concentration of no more than about 20%.5. The method of claim 4 , wherein said concentration is no more than about 10%.6. The method of claim 1 , wherein said ethanol is produced by a fermentation process.7. The method of claim 6 , wherein said ethanol is a component of a fermentation stream when contacted with said metal-loaded zeolite catalyst.8. (canceled)9. The method of claim 1 , wherein said temperature is at least 350° C. and up to 550° C.10. The method of claim 1 , wherein said temperature is at least 400° C. and up to 550° C.11. (canceled)12. The method of claim 1 , wherein said metal is selected from alkali metal claim 1 , alkaline earth metal claim 1 , copper claim 1 , iron claim 1 , vanadium claim 1 , zinc claim 1 , titanium claim 1 , cadmium claim 1 , gallium claim 1 , indium claim 1 , and combinations thereof.13. The method of claim 1 , wherein said metal is gallium or indium.14. The method of claim 1 , wherein said zeolite comprises a pentasil zeolite.15. The method of claim 14 , wherein said pentasil ...

NANO-SIZED ZEOLITE SUPPORTED CATALYSTS AND METHODS FOR THEIR PRODUCTION

According to one or more embodiments described, a zeolite supported catalyst may be synthesized by a process that includes combining a colloidal mixture with a metal oxide support material to form a support precursor material, processing the support precursor material to form a support material, and impregnating the support material with one or more metals to form the zeolite supported catalyst. The colloidal mixture may include nano-sized zeolite crystals, and the nano-sized zeolite crystals may have an average size of less than 100 nm. 2. The zeolite supported catalyst of claim 1 , where the zeolite supported catalyst has a pore volume of at least 0.45 mL/g3. The zeolite supported catalyst of claim 1 , where the zeolite supported catalyst has a pore size of at least 9.5 nm.4. The zeolite supported catalyst of claim 1 , where the metal catalyst material comprises one or more of WO claim 1 , MoO claim 1 , NiO claim 1 , and CoO.5. The zeolite supported catalyst of claim 1 , where the porous alumina comprises:a small pore size alumina having a pore volume of from 0.4 mL/g to 0.6 mL/g; anda large pore size alumina having a pore volume of from 0.8 mL/g to 1.2 mL/g.6. The zeolite supported catalyst of claim 5 , comprising:from 10 wt. % to 65 wt. % of the small pore size alumina; andfrom 15 wt. % to 25 wt. % of the large pore size alumina. This application is a divisional application of and claims priority to U.S. patent application Ser. No. 15/480,917, filed on Apr. 6, 2017, which claims priority to U.S. Provisional Application Ser. No. 62/320,938, filed Apr. 11, 2016, all of which are incorporated by reference.The present disclosure relates to catalysts for chemical conversion of petrochemical fuels. More specifically, the disclosure relates methods for preparing catalysts which may be utilized in hydroprocessing treatments.Hydrocracking is a versatile catalytic process that converts heavy oils to lighter products by aromatic saturation, cracking, and isomerization ...

HYDROCRACKING CATALYST

Process for preparing a hydrocracking catalyst carrier which process comprises subjecting a carrier comprising an amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10 to calcination at a temperature of from 700 to 900° C., hydrocracking catalyst carrier comprising amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10, the infrared spectrum of which catalyst has a peak at 3690 cm, substantially reduced peaks at 3630 cmand 3565 cmand no peak at 3600 cm, hydrocracking catalyst carrier comprising an amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10, which catalyst has an acidity as measured by exchange with perdeuterated benzene of at most 20 micromole/gram, hydrocracking catalyst derived from such carrier and hydrocracking process with the help of such catalyst. 1. A hydrocracking process for converting a hydrocarbon feedstock into lower boiling materials , wherein said process comprises:{'sup': −1', '−1', '−1', '−1, 'contacting said hydrocarbon feedstock and hydrogen at an elevated temperature and an elevated pressure with a hydrocracking catalyst within a hydrocracking reaction vessel having a reactor inlet and a reactor outlet, wherein said hydrocracking catalyst comprises, a Group VIII metal; a Group VIB metal; and a carrier, wherein said carrier comprises an amorphous binder in an amount in the range of from 30% wt to 98% wt based on the total weight of said carrier, a zeolite Y, having a silica-to-alumina molar ratio of at least 10, in an amount in the range of from 2% to 70% wt based on the total weight of said carrier, and a second zeolite component that is either zeolite beta or ZSM-5 in an amount up to 20% wt based on the total weight of said carrier, and wherein the infrared spectrum of said carrier has peaks at 3690 cm, 3630 cm, and 3565 cm, and no peak at 3600 cm.'}2. A process as recited in claim 1 , wherein said hydrocracking catalyst contains from 2 to 40 ...

PLATINUM ENCAPSULATED ZEOLITE HYDROCRACKING CATALYST AND METHODS OF MAKING SAME

Embodiments of the present disclosure are directed to hydrocracking catalysts and methods of making same. The hydrocracking catalyst comprises a platinum encapsulated zeolite having a crystallinity greater than 20% determined by X-ray powder diffraction analysis. 1. A method of producing a hydrocracking catalyst , in which the method comprises:adding sodium hydroxide, an aluminum compound, a salt having an anion and a cation, and a silicon compound to an aqueous solution to form an aqueous mixture;stirring the aqueous mixture;adding a platinum compound to the aqueous mixture to form a pre-catalyst mixture;heating the pre-catalyst mixture at from 80° C. to 200° C. for at least 24 hours, thereby crystalizing the pre-catalyst mixture to form the hydrocracking catalyst comprising platinum encapsulated zeolite.2. The method of claim 1 , wherein the zeolite is sodalite.3. The method of claim 1 , in which the hydrocracking catalyst comprises greater than 20% crystallinity determined by X ray powder diffraction analysis.4. The method of claim 1 , in which the aluminum compound comprises aluminum metal powder claim 1 , aluminum hydroxide claim 1 , sodium aluminate claim 1 , or combinations thereof.5. The method of claim 1 , in which the silicon compound comprises silica claim 1 , sodium silicate claim 1 , colloidal silica claim 1 , fumed silica claim 1 , or combinations thereof.6. The method of claim 1 , in which the salt comprises sodium chloride claim 1 , potassium dichromate claim 1 , calcium chloride claim 1 , sodium bisulfate claim 1 , copper sulfate claim 1 , or combinations thereof.7. The method of claim 1 , in which the platinum compound comprises a platinum salt selected from the group of Pt(NH)Cl claim 1 , PtCl claim 1 , PtCl claim 1 , (NH)2PtCl claim 1 , (NH)2Pt(NO) claim 1 , NaPtCl.6HO claim 1 , HPtCl.6HO claim 1 , NaPtCl.4HO claim 1 , (NH)2PtCl claim 1 , or combinations thereof.8. The method of claim 1 , in which the pre-catalyst mixture comprises xNaOH:1AlO3: ...

Catalyst for pyrolysis of feedstock

A novel catalyst blend for processing of feedstocks into monoaromatics in a single stage, comprising at least one cracking catalyst, one heterogeneous transition metal catalyst, and optionally at least one hydrogenation catalyst. The process occurs in one-step or single stage with substantially no solvents or external additives, or when the feedstock contains less than 15% oxygen, the process includes additional water or steam to enable sufficient amounts of H 2 being produced in-situ.

CATALYST COMPRISING AT LEAST ONE ZEOLITE NU-86, AT LEAST ONE ZEOLITE USY AND A POROUS MINERAL MATRIX AND PROCESS FOR HYDROCONVERSION OF HYDROCARBON FEEDS USING SAID CATALYST

The invention relates to a catalyst comprising at least one metal selected from the group formed by metals of group VIB and of group VIII of the periodic table, used alone or as a mixture, and a support comprising at least one zeolite NU-86, at least one zeolite Y and at least one porous mineral matrix containing at least aluminium and/or at least silicon. The invention also relates to a process for hydrocracking of hydrocarbon feeds employing said catalyst. 1. Catalyst comprising at least one metal selected from the group formed by metals of group VIB and of group VIII of the periodic table , used alone or as a mixture , and a support comprising at least one zeolite NU-86 , at least one zeolite Y and at least one porous mineral matrix containing at least aluminium and/or at least silicon.2. Catalyst according to in which said zeolite Y is a dealuminized zeolite called USY.3. Catalyst according to in which said porous mineral matrix is selected from transition aluminas claim 1 , doped aluminas claim 1 , silicalite and silicas claim 1 , aluminosilicates claim 1 , non-zeolitic crystalline molecular sieves claim 1 , alone or as a mixture.4. Catalyst according to in which said porous mineral matrix is selected from alumina and silica-alumina.5. Catalyst according to in which said catalyst comprises at least one hydrogenating-dehydrogenating metal of group VIB in combination with at least one group VIII base metal.6. Catalyst according to in which the content of group VIB metal claim 5 , in oxide equivalent claim 5 , is between 5 and 40 wt % relative to the total weight of said catalyst claim 5 , and the content of group VIII base metal claim 5 , in oxide equivalent claim 5 , is between 0.5 and 10 wt % relative to the total weight of said catalyst.7. Catalyst according to in which said catalyst comprises claim 1 , in wt % relative to the total weight of the catalyst:0.2 to 10%, of at least one zeolite NU-86,0.4 to 40%, of at least one zeolite Y,from 0.5 to 50% of at ...

Modified Y Molecular Sieve and Preparation Method and Use Thereof, Supported Catalyst, and Hydrocracking Method

The present invention discloses a modified Y molecular sieve, a preparation method and a use of the modified Y molecular sieve, a supported catalyst, and a hydrocracking method. The silica-alumina mole ratio in the surface layer of the modified Y molecular sieve is 20-100:1, and the silica-alumina mole ratio in the body phase of the modified Y molecular sieve is 8-30:1. When a hydrocracking catalyst prepared from the modified Y molecular sieve is used for hydrocracking, the hydrocracking catalyst has higher reactivity and higher nitrogen tolerance. The hydrocracking catalyst prepared from the modified Y molecular sieve is suitable for use for increasing the yield of diesel oil, increasing the yield of chemical materials, and catalyzed hydrogenation conversion of diesel oil, etc. 1. A modified Y molecular sieve , wherein the silica-alumina mole ratio in the surface layer of the modified Y molecular sieve is 20-100:1 , the silica-alumina mole ratio in the body phase of the modified Y molecular sieve is 8-30:1 , and the silica-alumina mole ratio in the surface layer of the modified Y molecular sieve is higher than the silica-alumina mole ratio in the body phase at least by 10.2. The modified Y molecular sieve according to claim 1 , wherein the silica-alumina mole ratio in the surface layer of the modified Y molecular sieve is higher than the silica-alumina mole ratio in the body phase by 20-70.3. The modified Y molecular sieve according to claim 1 , wherein the silica-alumina mole ratio in the surface layer is 30-80:1.4. The modified Y molecular sieve according to claim 1 , wherein the thickness of the surface layer is 10-200 nm.5. The modified Y molecular sieve according to claim 1 , wherein the surface layer is formed by in-situ dealumination claim 1 , and the grain size of the modified Y molecular sieve is 0.4-1.2 μm.6. The modified Y molecular sieve according to claim 1 , wherein the acid content measured by near infrared spectrometry (NIS) in the modified Y ...

METHOD FOR OPTIMIZING CATALYST LOADING FOR HYDROCRACKING PROCESS

The invention relates to a method for optimizing layered catalytic processes. This is accomplished by testing various catalysts with a compound found in a feedstock to be tested, to determine the facility of the catalyst in hydrogenating, hydrosulfurizing, or hydrodenitrogenating the molecule, and hence the feedstock. in a preferred embodiment, the Double Bond Equivalence of the feedstock and molecule are determined, and catalysts are pre-selected based upon their known ability to work with materials of this DBE value. 1. A method for optimizing a layered hydrocracking catalytic process , comprising (i) contacting a model compound capable of (a) being hydrocracked as well as at least one of (ii) hydrogenation , hydrosulfurization and hydrodenitrogenation to a plurality of catalysts to determine an optimal catalyst for each of (i) and (ii) , (b) followed by layering the optimal catalysts for each of (i) and (ii) in a reaction chamber based on their activity reacting with said model compound , and (c) contacting a feedstock to the layered catalysts under condition favoring formation of lower weight hydrocarbon from said hydrocarbon containing feedstock , wherein said model compound boils in the range of 180° C.-520° C. and is selected from the group consisting of methylnaphthalene , dibenzothiophene , an alkylated or naphthalated derivative thereof , a basic nitrogen compound and a carbazole molecule.2. (canceled)3. (canceled)4. The method of claim 1 , further comprising determining double bond equivalence (DBE) of said feedstock claim 1 , and contacting said model compound to a plurality of catalysts suitable for hydrocracking a substance with a DBE of said feedstock claim 1 , to determine an optimum hydrocracking catalyst for said feedstock.5. The method of claim 4 , further comprising contacting said model compound to a second plurality of catalysts suitable for hydrogenating claim 4 , hydrodesulfurizing claim 4 , or hydrodenitrogenating a substance with a DBE ...

PROCESS FOR PREPARING A HYDROCONVERSION CATALYST, CATALYST THUS OBTAINED AND USE THEREOF IN A HYDROCONVERSION PROCESS

The invention relates to a process for preparing a hydroconversion catalyst based on a modified zeolite of the FAU framework type with preserved crystallinity and microporosity, comprising the steps of: 1. Process for preparing a hydroconversion catalyst based on a modified zeolite of the FAU framework type with preserved crystallinity and interconnected trimodal porosity , comprising the steps of:A—preparation of a modified zeolite of the FAU framework type, whose intracrystalline structure presents at least one network of micropores, at least one network of small mesopores with a mean diameter of 2 to 5 nm and at least one network of large mesopores with a mean diameter of 10 to 50 nm; these various networks being interconnected;B—mixing the zeolite with a binder, shaping the mixture, and then calcining;C—impregnation of the shaped zeolite with at least one compound of a catalytic metal chosen from compounds of a metal from group VIII and/or from group VIB, in acidic medium, provided that at least one compound of a catalytic metal is soluble within said acidic medium and that the acid acts as a complexing or chelating agent for at least one compound of a catalytic metal.2. Process according to claim 1 , wherein the acidic medium contains water as solvent.3. Process according to claim 1 , wherein the acid is an organic oxygen- or nitrogen-containing compound that contains at least one carboxylic functional group and at least one additional function group selected from carboxylic claim 1 , hydroxyamic claim 1 , hydroxyl claim 1 , keto claim 1 , amino claim 1 , amido claim 1 , imino claim 1 , epoxy claim 1 , and thio claim 1 , preferably claim 1 , wherein the organic acid is citric acid claim 1 , thioglycolic acid claim 1 , maleic acid claim 1 , more preferably claim 1 , wherein the organic acid is citric acid.4. Process according to claim 1 , wherein the acid is an inorganic acid selected from the group of phosphorus-containing acids claim 1 , more preferably claim ...

Laboratory Process For Deactivation of A Porous Solid

A process for the laboratory deactivation of a porous solid comprising subjecting the porous solid to a cyclic treatment, the treatment being selected from a hydration/dehydration cyclic treatment, a thermal cyclic treatment, or combinations thereof. 1. A process for the laboratory deactivation of a porous solid comprising subjecting the porous solid to a cyclic treatment , the treatment being selected from a hydration/dehydration cyclic treatment , a thermal cyclic treatment , or combinations thereof , contacting in a hydration step the porous solid with a hydrating gas stream comprising water at a relative humidity of 20 to 100% and a temperature of 50° F. to 400° F., thereby forming a hydrated solid; and', 'contacting in a dehydration step the hydrated solid with a dehydrating gas stream comprising water at a relative humidity of less than 20%, and a temperature of from 200° F. to 1600° F., thereby forming a dehydrated solid,', 'wherein for each cycle, except the first cycle, the dehydrated solid is the porous solid for the hydration step in the next cycle; and, 'the hydration/dehydration cyclic treatment comprising at least five cycles of heating the porous solid to a heated temperature of 900° F. to 1575° F., thereby forming a heated porous solid; and', 'cooling the heated porous solid to a cooled temperature, thereby forming a cooled porous solid,', 'wherein the difference between the heated temperature and the cooled temperature is at least 200° F., and where for each cycle, except the first cycle, the cooled porous solid is the porous solid for the heating step in the next cycle., 'the thermal cyclic treatment comprising at least five cycles of2. The process of wherein the temperature of the hydration step is from 60 to 230° F.3. The process of wherein the temperature of the hydration step is from 100 to 225° F.4. The process of wherein the temperature of the dehydration step is from 500 to 1575° F.5. The process of wherein the temperature of the dehydration ...

Catalyst for pyrolysis of feedstock

A novel catalyst blend for processing of feedstocks into monoaromatics in a single stage, comprising at least one cracking catalyst, one heterogeneous transition metal catalyst, and optionally at least one hydrogenation catalyst. The process occurs in one-step or single stage with substantially no solvents or external additives, or when the feedstock contains less than 15% oxygen, the process includes additional water or steam to enable sufficient amounts of H 2 being produced in-situ.

PROCESS FOR THE PREPARATION OF A HYDROCRACKING CATALYST

This invention relates to a process for the preparation of a hydrocracking catalyst and its use. A zeolite Y having specifically defined properties is mixed with an alumina binder component and a first metals-containing solution that is extruded to form an extruded mixture. The extruded mixture is dried and calcined. The dried and calcined mixture is then impregnated with a second metals-containing solution. 1. A process for the preparation of a hydrocracking catalyst , which comprises the steps of:(a) mixing a zeolite Y having a unit cell size in the range of from 24.42 to 24.52 Å, a bulk silica to alumina molar ratio (SAR) in the range of from 10 to 15, and a surface area of from 910 to 1020 m2/g with an alumina binder component and two or more catalytically active metal components which metal components are contained in one or more solutions, wherein the zeolite Y is present in an amount of 40 wt. % or greater, based on the total weight of the zeolite Y and the alumina binder component;(b) extruding the mixture as obtained in step (a);(c) drying the extruded mixture as obtained in step (b);(d) calcining the dried and extruded mixture as obtained in step (c); and(e) mixing the calcined product as obtained in step (d) with two or more catalytically active metal components which metal components are contained in one or more solutions.2. A process according to claim 1 , wherein the impregnation in step (e) is carried out in the presence of a hydroxy carboxylic acid.3. A process according to claim 2 , wherein the hydroxy carboxylic acid comprises gluconic acid claim 2 , malic acid claim 2 , tartaric acid claim 2 , citric acid or a mixture thereof.4. A process according to claim 3 , wherein the hydroxy carboxylic acid is citric acid or malic acid.5. A process according to claim 2 , wherein the second metals-containing solution comprises the hydroxy carboxylic acid.6. A process according to claim 1 , wherein the first metals-containing solution and the second metals- ...

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 , ...

PROCESS FOR PREPARING A MESOPORIZED CATALYST, CATALYST THUS OBTAINED AND USE THEREOF IN A CATALYTIC PROCESS

A hydroconversion catalyst obtained by the process described, comprising a mesoporized zeolite with healed zeolitic structure, containing at least one network of micropores and at least one network of mesopores, having an atomic Si/Al ratio within the zeolite framework of greater than or equal to 2.3 and showing reduced amount of extra-framework aluminium with regard to that of a mesoporized zeolite with no healed zeolitic structure. 3. A process for the hydroconversion of a hydrocarbon feedstock claim 1 , wherein said feedstock to be treated is placed in contact with the hydroconversion catalyst according to . This application is a continuation application of U.S. application Ser. No. 14/347,159, filed on Mar. 25, 2014, which is a National Stage of International Application No. PCT/EP2012/071017 filed Oct. 24, 2012, claiming priority based on French Patent Application No. 11 59618 filed Oct. 24, 2011 and French Patent Application No. 11 62520 filed Dec. 29, 2011, the contents of all of which are incorporated herein by reference in their entirety.The invention relates to a process for preparing a mesopores-containing catalyst, the catalyst thus obtained and the use of the catalyst thus obtained in an industrial process.The catalyst described here comprises a mesoporized zeolite and may be used in many hydroconversion processes, in particular, in the hydrocracking process.The various zeolites are distinguished by different structures and properties, and are well known in the art. A few structures commonly used in the field of catalysis are disclosed in WO2010/072976, among them some are given below.Zeolite Y (FAU) is a three-dimensional zeolite with large pores, whose structure has large cavities interconnected by channels formed from 12-membered rings, each ring presenting 12 (Si and Al) cations and 12 O anions.Beta zeolite (BEA) is a three-dimensional zeolite with large pores comprising pores formed from 12-membered rings in all directions.Zeolite ZMS-5 (MFI) is a ...

CATALYTIC CONVERTER

In order to specify a catalytic converter, especially SCR catalytic converter, with maximum catalytic activity, this catalytic converter has at least one catalytically active component and additionally at least one porous inorganic filler component having meso- or macroporosity. The organic porous filler component has a proportion of about 5 to 50% by weight. More particularly, a diatomaceous earth or a pillared clay material is used as the porous inorganic filler component. 1. A catalytic converter comprising: (a) a base component comprising at least one catalytically active component , a binder component and optionally fibres that provide mechanical stability; and (b) at least one porous inorganic filler component , wherein the inorganic filler component has at least mesoporosity ,wherein the at least one porous filler component comprises a diatomaceous earth material.2. The catalytic converter according to claim 1 , wherein at least one catalytically active component is an SCR catalyst.3. The catalytic converter according to claim 1 , wherein:the at least one catalytically active component, the binder component, and the fibers, if present, are present in a defined ratio of proportions by weight relative to one another, andthe catalytic converter has at least a same catalytic activity as a comparative catalytic converter without a filler component and with the same catalytically active component, the binder component, and the fibers, if present, having same defined ratio of proportions relative to one another.4. The catalytic converter according to claim 1 , wherein the inorganic porous filler component is present within the range from 5 to 50% by weight relative to the total weight of the catalytic converter.5. The catalytic converter according to claim 4 , wherein the inorganic porous filler component is present within the range from 10 to 25% by weight claim 4 , relative to the weight of the catalytic converter.6. The catalytic converter according to claim 1 , ...

MODIFIED ZEOLITE SECOND STAGE HYDROCRACKING CATALYST AND USE OF THEREOF FOR HYDROCARBON CONVERSION

A hydrocracking catalyst, containing a USY zeolite modified by treatment with an organic acid to remove aluminum, an alumina binder, two or more metals selected from metals of Groups VIA and VIIIA, and cerium in the range of 0.1 to 5.0 wt %. 1. A hydrocracking catalyst , comprising: a USY zeolite modified by treatment with an organic acid to remove aluminum; an alumina binder; two or more metals selected from metals of Groups VIA and VIIIA; and cerium in the range of 0.1 to 5.0 wt %.2. The catalyst of claim 1 , wherein the metal of Group VIA is W.3. The catalyst of claim 1 , wherein the metal of Group VIIIA is Ni.4. The hydrocracking catalyst of claim 1 , wherein at least one of the metals of Group VIA and the metals of Group VIIIA is in sulfided form.5. The hydrocracking catalyst of claim 1 , wherein a Si/Al molar ratio of the USY zeolite is in the range of 6-10.6. The hydrocracking catalyst of claim 1 , wherein the amount of the USY zeolite is from 25 to 50 wt % based on the total weight of the catalyst.7. The hydrocracking catalyst of claim 1 , wherein the amount of the alumina binder is from 25 to 50 wt % based on the total weight of the catalyst.8. The hydrocracking catalyst of claim 1 , comprising WOin an amount of from 20 to 30 wt % based on a total weight of the catalyst.9. The hydrocracking catalyst of claim 1 , comprising NiO in an amount of 1 to 10 wt % based on a total weight of the catalyst.10. A process of hydrocracking claim 1 , comprising hydrocracking of a hydrotreated vacuum gas oil with the hydrocracking catalyst of . 1. Field of the DisclosureThe present invention relates to a USY catalyst, a method for modifying a USY zeolite, preparation of a hydrocracking catalyst, and its use for hydrocracking of petroleum fractions such as vacuum gas oil. The hydrocracking catalyst is employed for preparing valuable light and medium boiling range hydrocarbons from heavy hydrocarbons of vacuum gas oil fractions of crude oil.2. Description of Related ArtIn the ...

MIDDLE DISTILLATE HYDROCRACKING CATALYST CONTAINING ZEOLITE USY WITH ENHANCED ACID SITES

A hydrocracking catalyst is provided comprising: a) greater than 10 wt % of a zeolite USY having: i. a total OD acidity of 0.350 to 0.650 mmol/g; ii. an ASDI between 0.05 and 0.15; iii. a BET surface area greater than 600 m/g; iv. a SAR greater than 10; v. less than 45 vol % of pores greater than 2 nm; b) a support; and c) at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table. A process for hydrocracking using a hydrocracking catalyst to produce middle distillates is provided. A method for making a hydrocracking catalyst is also provided. 1. A hydrocracking catalyst comprising: i. a total OD acidity of 0.350 to 0.650 mmol/g;', 'ii. an ASDI between 0.05 and 0.15;', {'sup': '2', 'iii. a BET surface area greater than 600 m/g;'}, 'iv. a SAR greater than 10;', 'v. less than 45 vol % of pores greater than 2 nm;, 'a. greater than 10 wt % of a zeolite USY havingb. a support; andc. at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table;wherein the hydrocracking catalyst is conducive to making middle distillates.2. The hydrocracking catalyst of claim 1 , wherein the hydrocracking catalyst has at least 7° F. (4° C.) more activity than a comparable hydrocracking catalyst comprising a different zeolite USY with a lower total OD acidity of at most 0.34 mmol/g.3. The hydrocracking catalyst of claim 1 , wherein the hydrocracking catalyst has improved selectivity for producing a hydrocracked effluent having a TBP of 250-550° F. (121-288° C.) compared to a comparable hydrocracking catalyst comprising a different zeolite USY with a higher ASDI of 0.16 or greater.4. The hydrocracking catalyst of claim 1 , wherein the total OD acidity is from 0.450 to 0.600 mmol/g.5. The hydrocracking catalyst of claim 1 , wherein the zeolite USY has a unit cell size from 24.20 to 24.50 Å.6. The hydrocracking catalyst of claim 5 , wherein the unit cell size is from ...

MIDDLE DISTILLATE HYDROCRACKING CATALYST WITH A BASE EXTRUDATE HAVING A HIGH NANOPORE VOLUME

The present invention is directed to an improved hydrocracking catalyst containing a amorphous silica-alumina (ASA) base and alumina support. The ASA base is characterized as having a high nanopore volume and low particle density. The alumina support is characterized as having a high nanopore volume. Hydrocracking catalysts employing the combination high nanopore volume ASA base and alumina support exhibit improved hydrogen efficiency, and greater product yield and quality, as compared to hydrocracking catalysts containing conventional ASA base and alumina components. 1. A hydrocracking catalyst , comprising:a base extrudate comprising at least one molecular sieve, an alumina and an amorphous silica alumina support, wherein the base extrudate has a nanopore volume in the 6 nm to 11 nm range of 0.5 to 0.9 cc/g; andat least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table.2. The hydrocracking catalyst of claim 1 , wherein the base extrudate is formed using an alumina having a nanopore volume in the 6 nm to 11 nm range of 0.1 to 0.3 cc/g.3. The hydrocracking catalyst of claim 2 , wherein the base extrudate is formed using an amorphous silica alumina support having a nanopore volume in the 6 nm to 11 nm range of 0.6 to 0.9 cc/g.4. The hydrocracking catalyst of claim 1 , wherein the base extrudate is formed using an amorphous silica alumina support having a nanopore volume in the 6 nm to 11 nm range of 0.6 to 0.9 cc/g.5. The hydrocracking catalyst of claim 1 , wherein the base extrudate has a total nanopore volume in the 2 to 50 nm of 0.7 to 1.2 cc/g.6. The hydrocracking catalyst of claim 1 , wherein the base extrudate has a particle density of 0.7 to 0.9 cc/g.7. A method for making a hydrocracking catalyst claim 1 , comprising the steps of:forming a base extrudate comprising at least one molecular sieve, an alumina and an amorphous silica alumina support, wherein the base extrudate has a nanopore volume ...

MIDDLE DISTILLATE HYDROCRACKING CATALYST MANUFACTURED USING A HIGH NANOPORE VOLUME AMORPHOUS SILICA-ALUMINA SUPPORT

The present invention is directed to an improved hydrocracking catalyst containing a amorphous silica-alumina (ASA) base and alumina support. The ASA base is characterized as having a high nanopore volume and low particle density. The alumina support is characterized as having a high total nanopore volume. Hydrocracking catalysts employing the combination high nanopore volume ASA base and alumina support exhibit improved hydrogen efficiency, and greater product yield and quality, as compared to hydrocracking catalysts containing conventional ASA base and alumina components. 1. A hydrocracking catalyst , comprising:a base extrudate comprising at least one molecular sieve, an alumina and an amorphous silica alumina support, wherein the base extrudate is formed using an amorphous silica alumina support having a nanopore volume in the 6 nm to 11 nm range of 0.6 to 0.9 cc/g; andat least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table.2. The hydrocracking catalyst of claim 1 , wherein the base extrudate is formed using an alumina having a nanopore volume in the 6 nm to 11 nm range of 0.1 to 0.3 cc/g.3. The hydrocracking catalyst of claim 1 , wherein the base extrudate has a particle density of 0.7 to 0.9 cc/g.4. The hydrocracking catalyst of claim 1 , wherein the base extrudate has a nanopore volume in the 6 nm to 11 nm range of 0.5 to 0.9 cc/g.5. The hydrocracking catalyst of claim 1 , wherein the base extrudate has a total nanopore volume in the 2 to 50 nm of 0.7 to 1.2 cc/g.6. A method for making a hydrocracking catalyst claim 1 , comprising the steps of:forming a base extrudate comprising at least one molecular sieve, an alumina and an amorphous silica alumina support, wherein the base extrudate is formed using an amorphous silica alumina support having a nanopore volume in the 6 nm to 11 nm range of 0.6 to 0.9 cc/g; andimpregnating the base extrude with at least one metal selected from the group ...

SUPPORTED CATALYSTS FOR PRODUCING ULTRA-LOW SULPHUR FUEL OILS

The present invention relates to the preparation of catalysts used in the hydrodesulfurization of fossil fuels and proposes a method for preparing thermally stable, low-cost catalysts for the hydrodesulfurization of petrol and diesel, based on highly active CoMo and NiMo. The catalyst for the hydroprocessing of gasoil or petrol in the present invention comprises a precursor which consists of chemical compounds obtained from organic acids and metal salts, and a support containing an ultra-stable Y-type zeolite useful in the hydroprocessing of heavy gas oil and/or light cyclic gas oil with high conversion rates. 1. A catalyst for gasoil or gasoline hydrotreating comprising a precursor consisting of chemical compounds obtained from organic acids and metal salts , and a support comprising an ultra-stable Y-type zeolite.2. The catalyst according to claim 1 , wherein the precursor consists of chemical compounds obtained from organic acids and metal salts of Group 6 of periodic table to generate bimetallic organometallic complexes.3. The catalyst according to claim 2 , wherein the chemical compounds obtained from organic acids are selected from the group consisting of malic acid claim 2 , oxalic acid and/or citric acid.4. The catalyst according to claim 2 , wherein the metal salts of Group 6 of periodic table are selected from the group consisting of molybdenum trioxide claim 2 , molybdic acid claim 2 , ammonium heptamolybdate claim 2 , equivalent compounds of tungsten and metal salts of Group 9 or 10.5. The catalyst according to claim 1 , wherein the support contains from 3 to 20% of and ultra-stable Y-type zeolite.6. The catalyst according to claim 5 , wherein the support contains from 5 to 10% of an ultra-stable Y-type zeolite.7. The catalyst according to claim 1 , wherein the support consists of an alumina-zeolite support with a specific surface area from 280 to 680 mg claim 1 , a pore volume from 0.4 to 0.9 cmgand an average pore diameter from 3 to 10 nm.8. The ...

Metathesis catalyst on mixed metal oxide-zeolite support and process for use thereof

The present invention relates to catalyst comprising at least one transition metal selected from Group VIA and Group VITA metals and a support containing a mixture of 0.1 to 60 percent by weight of zeolite, based on total weight of the support, with at least one other inorganic or organic material, wherein the at least one other inorganic or organic material is selected from silicon dioxide, titanium dioxide, zirconium dioxide and activated carbon, preferably silicon dioxide; and a process for olefin metathesis utilizing that catalyst.

METHOD FOR PRODUCING OLIGOSILANE

A method for producing an oligosilane which includes a reaction step of producing an oligosilane by dehydrogenative coupling of hydrosilane. The reaction step is carried out in the presence of a catalyst containing at least one transition element selected from the group consisting of Periodic Table group 3 transition elements, group 4 transition elements, group 5 transition elements, group 6 transition elements, and group 7 transition elements. Also disclosed is a method for producing a catalyst for dehydrogenative coupling that produces an oligosilane by dehydrogenative coupling of hydrosilane. 1. A method for producing an oligosilane , comprising a reaction step of producing an oligosilane by dehydrogenative coupling of hydrosilane , whereinthe reaction step is carried out in the presence of a catalyst containing at least one transition element selected from the group consisting of Periodic Table group 3 transition elements, group 4 transition elements, group 5 transition elements, group 6 transition elements, and group 7 transition elements.2. The method for producing an oligosilane according to claim 1 , wherein the catalyst is a heterogeneous catalyst containing a support and contains the transition element on the surface and/or in the interior of the support.3. The method for producing an oligosilane according to claim 2 , wherein the support is at least one selected from the group consisting of silica claim 2 , alumina claim 2 , titania claim 2 , and zeolite.4. The method for producing an oligosilane according to claim 3 , wherein the zeolite has pores with a minor diameter of at least 0.43 nm and a major diameter of not more than 0.69 nm.5. The method for producing an oligosilane according to claim 3 , wherein the support is a spherical or cylindrical molding claim 3 , of an alumina-containing powder as a binder and a zeolite having pores with a minor diameter of at least 0.43 nm and a major diameter of not more than 0.69 nm claim 3 , and has an alumina ...

Method of Forming a Catalyst with an Ion-Modified Binder

An alkylation catalyst having a zeolite catalyst component and a binder component providing mechanical support for the zeolite catalyst component is disclosed. The binder component is an ion-modified binder that can include metal ions selected from the group consisting of Co, Mn, Ti, Zr, V, Nb, K, Cs, Ga, B, P, Rb, Ag, Na, Cu, Mg, Fe, Mo, Ce, and combinations thereof. The metal ions reduce the number of acid sites on the zeolite catalyst component. The metal ions can range from 0.1 to 50 wt % based on the total weight of the ion-modified binder. Optionally, the ion-modified binder is present in amounts ranging from 1 to 80 wt % based on the total weight of the catalyst. 1. An alkylation catalyst , comprising:a catalyst component; anda binder component providing mechanical support for the catalyst component;wherein the binder component comprises an ion-modified binder comprising metal ions;wherein the metal ions are selected from the group consisting of Co, Mn, Ti, Zr, V, Nb, K, Cs, Ga, B, P, Rb, Ag, Na, Cu, Mg, Fe, Mo, Ce, and combinations thereof; andwherein the metal ions reduce the number of acid sites on the catalyst component.2. The catalyst of claim 1 , wherein the ion-modified binder comprises metal ions in amounts ranging from 0.1 to 50 wt % based on the total weight of the ion-modified binder.3. The process of claim 1 , wherein the ion-modified binder comprises metal ions in amounts ranging from 0.1 to 20 wt % based on the total weight of the ion-modified binder.4. The catalyst of claim 1 , wherein the ion-modified binder is present in amounts ranging from 1 to 80 wt % based on the total weight of the catalyst.5. The catalyst of claim 1 , wherein the ion-modified binder is present in amounts ranging from 5 to 60 wt % based on the total weight of the catalyst.6. The catalyst of claim 1 , wherein the metal ions on the ion-modified binder alters the spacial structure of the catalyst.7. The catalyst of claim 1 , wherein the binder comprises amorphous silica or ...

Catalyst For Preparing Chlorine Gas By Hydrogen Chloride Oxidation, And Preparation Method And Application Thereof

A catalyst for preparing chlorine gas by hydrogen chloride oxidation, comprising the following components calculated according to mass content based on the total weight of the catalyst: 0.5-20 wt % copper; 2-10 wt % manganese; 0.05-2 wt % boron; 0.01-3 wt % chromium; 0.1-10 wt % rare earth metal; 0.1-10 wt % potassium; and 3-15 wt % titanium; also comprising 0.02-1.1 wt % phosphorus; and 0.03-1.9 wt % iron; the carrier content is 55-90 wt %. In the case of a fluidized bed reactor, the present catalyst can achieve a one-way hydrogen chloride conversion rate of 80-85%. Almost all of the 0-1000 mg/kg of chlorinated benzene contained in hydrogen chloride gas can be converted into COand HO without generating polychlorinated benzene. 1. A catalyst for preparing chlorine gas by hydrogen chloride oxidation , wherein the catalyst comprises a copper element , a manganese element , a boron element , a chromium element , a rare earth element , a potassium element , a titanium element , a phosphorus element , an iron element and a carrier.2. The catalyst according to claim 1 , wherein based on the total mass of the catalyst claim 1 , the content of each element in the catalyst is: copper claim 1 , 0.5-20 wt % claim 1 , preferably 2-10%; manganese claim 1 , 2-10 wt % claim 1 , preferably 2-5 wt % claim 1 , boron claim 1 , 0.05-2 wt % claim 1 , preferably 0.06-1.0 wt %; chromium claim 1 , 0.01-3.0 wt % claim 1 , preferably 0.02-2.0 wt %; rare earth metal claim 1 , 0.1-10 wt % claim 1 , preferably 0.5-3.0 wt %; potassium claim 1 , 0.1-10 wt % claim 1 , preferably 0.2-2.5 wt %; titanium claim 1 , 3-15 wt % claim 1 , preferably 4-14 wt %; phosphorus claim 1 , 0.02-1.1 wt % claim 1 , preferably 0.03-0.50 wt %; iron claim 1 , 0.03-1.9 wt % claim 1 , preferably 0.04-1.0 wt %; the content of the carrier is 55-90 wt % claim 1 , preferably 70-90 wt %.3. The catalyst according to claim 1 , wherein the rare earth metal element is one or both of cerium and lanthanum.4. The catalyst according ...

Metathesis catalyst and process for producing olefin

The present invention provides a catalyst comprising a transition metal, an inorganic support, a zeolite, and a layered double hydroxide. Using of the catalyst according to the present invention in an olefin production process exhibits high activity and high selectivity with decreased deactivation rate, therefore longer reaction cycle can be performed and catalyst life is prolonged.

MODIFIED Y-TYPE MOLECULAR SIEVE AND PREPARATION METHOD THEREOF, HYDROCRACKING CATALYST AND PREPARATION METHOD THEREOF, AND METHOD FOR HYDROCRACKING HYDROCARBON OIL

A modified Y-type molecular sieve contains 0.5-2 wt. % of NaO based on the total amount of the modified Y-type molecular sieve. In the modified Y-type molecular sieve, the ratio between the total acid amount measured by pyridine and infrared spectrometry and total acid amount measured by n-butyl pyridine and infrared spectrometry is 1-1.2. The total acid amount measured by pyridine and infrared spectrometry of the modified Y-type molecular sieve is 0.1-1.2 mmol/g. The acid center sites of the molecular sieve of the modified Y-type molecular sieve are distributed in the large pore channels. The molecular sieve is used in the hydrocracking reaction process of a wax oil. 1. A modified Y-type molecular sieve , containing 0.5-2 wt. % of NaO based on the total amount of the modified Y-type molecular sieve; the ratio between the total acid amount measured by pyridine and infrared spectrometry of the modified Y-type molecular sieve and total acid amount measured by n-butyl pyridine and infrared spectrometry of the modified Y-type molecular sieve is 1-1.2; the total acid amount measured by pyridine and infrared spectrometry of the modified Y-type molecular sieve is 0.1-1.2 mmol/g.2. The modified Y-type molecular sieve of claim 1 , wherein the modified Y-type molecular sieve contains 0.8-1.8 wt. % of NaO based on the total amount of the modified Y-type molecular sieve; the ratio between the total acid amount measured by pyridine and infrared spectrometry of the modified Y-type molecular sieve and total acid amount measured by n-butyl pyridine and infrared spectrometry of the modified Y-type molecular sieve is 1.02-1.15; the total acid amount measured by pyridine and infrared spectrometry of the modified Y-type molecular sieve is 0.2-1 mmol/g.3. The modified Y-type molecular sieve of claim 2 , wherein the modified Y-type molecular sieve contains 1-1.5 wt. % of NaO based on the total amount of the modified Y-type molecular sieve; the ratio between the total acid amount measured ...

HYDROPROCESSING CATALYST COMPOSITION AND PROCESS THEREOF

The present invention relates to a catalyst precursor composition comprising a first component having active sites, said first component being at least one of the surface modified clay and/or pore modified zeolite; and a second component being metal species comprising of at least one metal selected from Group VI B and at least one metal selected from VIII B and the second component is in intimate contact with the active sites of the first component. The present invention also provides a process for preparing the catalyst precursor composition. The present invention also relates to a catalyst composition and process of preparation thereof by using the catalyst precursor. More particularly, the present invention provides a catalyst composition suitable for converting hydrocarbon feeds to diesel range product. 2. The catalyst precursor composition as claimed in claim 1 , wherein the second component is present in an amount of 1 to 30 wt % claim 1 , of the total weight of the catalyst precursor composition.3. The catalyst precursor composition as claimed in claim 2 , wherein the second component is present in an amount of 5 to 25 wt % of the total weight of the catalyst precursor composition.4. The catalyst precursor composition as claimed in claim 2 , wherein the second component is present in an amount of 10 to 20 wt % of the total weight of the catalyst precursor composition.5. The catalyst precursor composition as claimed in any of the preceding claims claim 2 , wherein the ratio of Group VIII B metal to total metal component comprising both Group VIB and VIIIB metals is from 0.1:1 to 0.5:1.6. The catalyst precursor composition as claimed in claim 1 , wherein the first component comprises both the surface modified clay and the pore modified zeolite.7. The catalyst precursor composition as claimed in claim 6 , wherein the ratio by weight of the surface modified clay to the pore modified zeolite is in the range of 1:1 to 9:1.8. The catalyst precursor composition as ...

DIESEL OXIDATION CATALYST

An oxidation catalyst composite, methods, and systems for the treatment of exhaust gas emissions from a diesel engine are described. More particularly, described is an oxidation catalyst composite including a first oxidation component comprising a first refractory metal oxide support, palladium (Pd) and platinum (Pt); a NOstorage component comprising one or more of alumina, silica, titania, ceria, or manganese; and a second oxidation component comprising a second refractory metal oxide, a zeolite, and Pt. The oxidation catalyst composite is sulfur tolerant, adsorbs NOand thermally releases the stored NOat temperature less than 350° C. 120-. (canceled)21. A method for treating a diesel engine exhaust gas stream , the method comprising contacting an exhaust gas stream with an oxidation catalyst composite , and passing the exhaust gas stream through a downstream SCR catalyst , wherein the oxidation catalyst composite comprises:a carrier substrate; and a first oxidation component comprising at least one platinum group metal (PGM) and a first refractory metal oxide, wherein the first oxidation component is substantially free of zeolite;', {'sub': 'x', 'a NOstorage component comprising one or more of alumina, silica, titania, ceria, and manganese; and'}, 'a second oxidation component comprising a second refractory metal oxide, a zeolite, and at least one PGM., 'a catalytic coating on at least a portion of the carrier substrate, the catalytic coating including22. The method of claim 21 , wherein the downstream SCR catalyst is disposed on a wall flow filter monolith.23. A system for treatment of a lean burn engine exhaust gas stream comprising hydrocarbons claim 21 , carbon monoxide claim 21 , nitrogen oxides claim 21 , particulate matter claim 21 , and other exhaust components claim 21 , the system comprising:an exhaust conduit in fluid communication with a lean burn engine via an exhaust manifold;an oxidation catalyst composite; anda catalyzed soot filter and an SCR ...

FILTER FOR FILTERING PARTICULATE MATTER FROM EXHAUST GAS EMITTED FROM A COMPRESSION IGNITION ENGINE

A filter for filtering particulate matter (PM) from exhaust gas emitted from a compression ignition engine, which filter comprising a porous substrate having inlet surfaces and outlet surfaces, wherein the inlet surfaces are separated from the outlet surfaces by a porous structure containing pores of a first mean pore size, wherein the porous substrate is coated with a wash coat comprising a plurality of solid particles comprising a molecular sieve promoted with at least one metal wherein the porous structure of the wash coated porous substrate contains pores of a second mean pore size, and wherein the second mean pore size is less than the first mean pore size. 1. A filter for filtering particulate matter (PM) from an exhaust gas , the filter comprising:a. a wall flow filter having inlet and outlet surfaces and a porous substrate between the inlet and outlet surfaces, wherein the porous substrate has pores of a first mean pore size,b. a first washcoat coated on the inlet and/or outlet surface of the porous wall flow substrate and within the wall flow substrate, wherein the first washcoat has a second mean pore size that is less than the first mean pore size,wherein the filter further comprises a layer of a second washcoat, wherein the first washcoat and second washcoat layer have different formulations and wherein substantially none of the second washcoat enters the wall flow substrate, andwherein at least one of the first and second washcoats comprise a metal selected from Cu, Fe, Ce, Pt, Pd, or Rh.2. The filter of claim 1 , wherein the second washcoat layer is coated on the outlet surface of the wall flow filter.3. The filter of claim 1 , wherein the second washcoat layer is coated on the outlet surface of the wall flow filter.4. The filter of claim 1 , wherein either one or both of the inlet and outlet surfaces of the wall flow filter comprise a plurality of washcoat layers comprising the first washcoat layer and the second washcoat layer.5. The filter of claim ...

Hydrocracking Catalyst Containing Zeolite USY and Low Acidity and Large Domain Size Zeolite Beta

A hydrocracking catalyst comprising a zeolite beta having an average domain size from 800 to 1500 nm; a zeolite USY; a catalyst support; and at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table. The zeolite beta has an OD acidity of 20 to 50 μmol/g and the catalyst support comprises an amorphous silica aluminate and a second support material when the weight percentage content of the zeolite beta is less than the weight percentage of the zeolite USY, and, when the weight percentage content of the zeolite beta is greater than the weight percentage of the zeolite USY, the zeolite beta has an OD acidity of 20 to 400 μmol/g, the zeolite beta content is from 0.5 to 10 wt. % and the zeolite USY has an ASDI between 0.05 and 0.12 with a corresponding zeolite USY content of from 0 to 5 wt. %. A process for hydrocracking a hydrocarbonaceous feedstock using the catalyst is also described as is a method for making the hydrocracking catalyst. 1. A hydrocracking catalyst comprising:{'sup': '2', 'a zeolite beta having an average domain size from 800 to 1500 nm;'}a zeolite USY;a catalyst support; andat least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table, the zeolite beta has an OD acidity of 20 to 50 μmol/g and the catalyst support comprises an amorphous silica aluminate and a second support material when the weight percentage content of the zeolite beta is less than the weight percentage of the zeolite USY; and', 'the zeolite beta has an OD acidity of 20 to 400 μmol/g and the zeolite beta content is from 0.5 to 10 wt. % and the zeolite USY has an ASDI between 0.05 and 0.12 and the zeolite USY content is from 0 to 5 wt. % when the weight percentage content of the zeolite beta is greater than the weight percentage of the zeolite USY., 'wherein,'}2. The hydrocracking catalyst of claim 1 , wherein the zeolite beta has a SiO/AlOratio (SAR) from 50 ...

METHOD FOR HYDROCRACKING HYDROCARBON FEEDSTOCKS USING A CATALYST COMPRISING A ZEOLITE AND AN AMORPHOUS MESOPOROUS ALUMINA

The present invention describes a process for hydrocracking at least one hydrocarbon feed in which at least 50% by weight of the compounds have an initial boiling point of more than 300° C. and a final boiling point of less than 540° C. using at least one catalyst comprising at least one metal from group VIB and/or at least one metal from group VIII of the periodic classification of the elements and a support comprising at least one zeolite containing at least one series of channels the opening of which is defined by a ring containing 12 oxygen atoms (12MR), and at least one binder, said support being prepared from a highly dispersible alumina gel, said hydrocracking process being operated at a temperature in the range 200° C. to 480° C., at a total pressure in the range 1 MPa to 25 MPa, with a ratio of the volume of hydrogen to the volume of hydrocarbon feed in the range 80 to 5000 litres per litre and with an hourly space velocity (HSV), defined as the ratio of the volume flow rate of liquid hydrocarbon feed to the volume of catalyst charged into the reactor, in the range 0.1 to 50 h. 1. A process for hydrocracking at least one hydrocarbon feed in which at least 50% by weight of the compounds have an initial boiling point of more than 300° C. and a final boiling point of less than 540° C. , at a temperature in the range 200° C. to 480° C. , at a total pressure in the range 1 MPa to 25 MPa , with a ratio of the volume of hydrogen to the volume of hydrocarbon feed in the range 80 to 5000 litres per litre and with an hourly space velocity (HSV) , defined as the ratio of the volume flow rate of liquid hydrocarbon feed to the volume of catalyst charged into the reactor , in the range 0.1 to 50 h , said process using at least one catalyst comprising at least one metal from group VIB and/or at least one metal from group VIII of the periodic classification and a support comprising at least one zeolite containing at least one series of channels the opening of which is ...

HYDROCARBON CONVERSION PROCESS

The present invention relates to a hydrocarbon conversion process comprising contacting a hydrocarbon feed stream with a hydrocarbon conversion catalyst, wherein the hydrocarbon conversion catalyst comprises a first composition comprising a dehydrogenation drogenation active metal on a solid support; and a second composition comprising a transition metal and a doping agent on an inorganic support, wherein the doping agent is selected from zinc, gallium, indium, lanthanum, and mixtures thereof. 1. A hydrocarbon conversion process comprising contacting a hydrocarbon feed stream with a hydrocarbon conversion catalyst , wherein the hydrocarbon conversion catalyst comprises:a first composition comprising a dehydrogenation active metal on a solid support; anda second composition comprising a transition metal and a doping agent on an inorganic support, wherein the doping agent is selected from zinc, gallium, indium, lanthanum, and mixtures thereof.2. The hydrocarbon conversion process according to claim 1 , wherein the dehydrogenation active metal is selected from platinum claim 1 , palladium claim 1 , iridium claim 1 , chromium claim 1 , and mixtures thereof.3. The hydrocarbon conversion process according to claim 1 , wherein the solid support is selected from aluminium oxide claim 1 , silicon dioxide claim 1 , zirconium dioxide claim 1 , titanium dioxide claim 1 , magnesium oxide claim 1 , calcium oxide claim 1 , and mixtures thereof.4. The hydrocarbon conversion process according to claim 1 , wherein the transition metal is selected from molybdenum claim 1 , tungsten claim 1 , rhenium claim 1 , and mixtures thereof.5. The hydrocarbon conversion process according to claim 1 , wherein the inorganic support is selected from aluminium oxide claim 1 , silicon dioxide claim 1 , zirconium dioxide claim 1 , titanium dioxide claim 1 , zeolite claim 1 , and mixtures thereof.6. The hydrocarbon conversion process according to claim 1 , wherein the second composition further ...

Method for the catalytic conversion of glycerol to propanol

In a method, device, catalyst and a method for producing a catalyst for the catalytic conversion of a substance mixture containing glycerol to propanol in a fixed-bed reactor, substrates of the catalyst have inorganic materials and/or metal oxides. The substrates have a pore diameter at the surface of between 10 and 25 angstroms, preferably between 12 and 20 angstroms, particularly preferably 15 angstroms.

制备和形成负载活性金属的催化剂和前体的方法

本发明涉及制备负载型催化剂的方法，所述方法包括以下步骤：（i）提供多孔催化剂载体，其包括具有包括一个或多个孔的内部孔结构的框架，所述内部孔结构包括沉淀剂；（ii）使催化剂载体与含有催化活性金属的溶液或胶态悬浮液接触，使得在与沉淀剂接触时，含有催化活性金属的颗粒沉淀在催化剂载体的框架的内部孔结构中。本发明还涉及根据以上方法制备的负载型催化剂，以及该催化剂在催化化学反应中的用途，例如，在烃类的费托合成中的用途。

Process for the production of glycolic acid

Un proceso para la producción de ácido glicólico en presencia de agua que comprende la puesta en contacto demonóxido de carbono y formaldehído con un catalizador que comprende un compuesto de polioxometalato ácidoencapsulado dentro de los poros de una zeolita, caracterizado por que la zeolita tiene jaulas más grandes que elcompuesto de polioxometalato ácido, y tiene poros con un diámetro más pequeño que el diámetro del compuesto depolioxometalato ácido. A process for the production of glycolic acid in the presence of water comprising contacting carbon monoxide and formaldehyde with a catalyst comprising an acid polyoxomethalate compound encapsulated within the pores of a zeolite, characterized in that the zeolite has larger cages than the compound of acid polyoxomethalate, and it has pores with a diameter smaller than the diameter of the acid depolyoxometalate compound.

Enhanced catalyst and process for converting synthesis gas to liquid motor fuels

The conversion of synthesis gas to liquid molar fuels by means of a cobalt Fischer-Tropsch catalyst composition is enhanced by the addition of molybdenum, tungsten or a combination thereof as an additional component of said composition. The presence of the additive component increases the olefinic content of the hydrocarbon products produced. The catalyst composition can advantageously include a support component, such as a molecular sieve, co-catalyst/support component or a combination of such support components.

Hydrocarbon conversion catalysts

Composition of matter suitable as a catalyst (base) in hydro­processing comprising a crystalline aluminosilicate zeolite and a binder wherein the crystalline aluminosilicate comprises a modified Y zeolite having a unit cell size below 24.35 Å, a degree of crystallinity which is at least retained at increasing SiO₂/Al₂O₃ molar ratios, a water adsorption capacity (at 25 °C and a p/p o value of 0.2) of at least 8% by weight of modified zeolite and a pore volume of at least 0.25 ml/g wherein between 10% and 60% of the total pore volume is made up of pores having a diameter of at least 8 nm. The invention also relates to hydroconversion catalysts and processes based on said compositions of matter.

A hydrogenation catalyst and use thereof

A hydrogenation catalyst comprises a support, metal active components consisting of Ni, Mo and W which are carried on the support, and auxiliary active components selected from the group consisting of F , P or their combination. Another hydrogenation catalyst comprises a support having molecular sieve component, metal active components consisting of Ni, Mo and W which are carried on the support . The catalysts can be used in methods for hydrogenation of hydrocarbon oil .The catalysts have higher catalytic activity than conventional catalysts.

Enhanced catalyst for converting synthesis gas to liquid motor fuels

The conversion of synthesis gas to liquid molar fuels by means of a cobalt Fischer-Tropsch catalyst composition is enhanced by the addition of molybdenum, tungsten or a combination thereof as an additional component of said composition. The presence of the additive component increases the olefinic content of the hydrocarbon products produced. The catalyst composition can advantageously include a support component, such as a molecular sieve, co-catalyst/support component or a combination of such support components.

Methods of preparation and forming supported active metal catalysts and precursors

The invention relates to a method of preparing a supported catalyst, which method comprises the steps of; (i) providing a porous catalyst support comprising a framework having an internal pore structure comprising one or more pores which internal pore structure comprises a precipitant; (ii) contacting the catalyst support with a solution or colloidal suspension comprising a catalytically active metal such that, on contact with the precipitant, particles comprising the catalytically active metal are precipitated within the internal pore structure of the framework of the catalyst support. The invention also relates to supported catalysts made according to the above method, and to use of the catalysts in catalysing chemical reactions, for example in the Fischer Tropsch synthesis of hydrocarbons.

A hydrogenation catalyst and its application

catalysts for vacuum gas demetalized mixture hydrocracking

CATALISADORES PARA HIDROCRAQUEAMENTO DE MISTURA DESMETALIZADA DE GASàLEO DE VÁCUO. Essa invenção se refere a um catalisador e a um processo de tratamento de hidrocarbonetos pesados utilizando o catalisador, O catalisador é útil para o tratamento de hidrocarbonetos pesados, óleo desmetalizado (DM0) e é particularmente útil na mistura de hidrocarboneto VGO/DMO. É útil também para DAO. O catalisador age para converter cataliticamente a mistura VGO/DMO em produtos de hidrocarboneto valiosos de cadeia menor. O catalisador inclui um material de suporte catalítico, um metal catalítico impregnado sobre o material de suporte catalítico, e um metal promotor no material de suporte catalítico para melhorar a conversão catalítica. A combinação do material de suporte catalítico com o metal catalítico e o metal promotor é operável para converter cataliticamente o VGO/DMO em produtos de hidrocarboneto possuindo cadeias de carbono menores. CATALYZERS FOR DEMETALIZED VACUUM GAS MIXER HYDROCRACKING. This invention relates to a catalyst and a process of treating heavy hydrocarbons using the catalyst. The catalyst is useful for treating heavy hydrocarbons, demetallized oil (DM0) and is particularly useful in the VGO / DMO hydrocarbon mixture. It is also useful for DAO. The catalyst acts to catalytically convert the VGO / DMO mixture into valuable lower chain hydrocarbon products. The catalyst includes a catalytic support material, a catalytic metal impregnated on the catalytic support material, and a promoter metal in the catalytic support material to enhance catalytic conversion. The combination of catalytic support material with catalytic metal and promoter metal is operable to catalytically convert VGO / DMO into hydrocarbon products having smaller carbon chains.

Magnesium aluminosilicate clays-synthesis and catalysis

This invention is directed to a synthesis process for preparing magnesium aluminosilicate clays and to the products of said process. Briefly, a silicon component, an aluminum component, and a magnesium component are combined, under aqueous conditions and at an acidic pH, to form a first reaction mixture and subsequently the pH of the first reaction mixture is adjusted to greater than 7.5 to form a second reaction mixture. The second reaction mixture is allowed to react under conditions sufficient to form the magnesium aluminosilicate clay of the present invention. The invention is also directed to catalyst compositions comprising the magnesium aluminosilicate clays synthesized according to the process of the invention. The resulting magnesium aluminosilicate clay can be used as a catalyst or as a component in catalyst compositions. The invention is further directed to a magnesium aluminosilicate clay with a characteristic 29 Si NMR spectrum and the use of said magnesium aluminosilicate clay in catalyst compositions.

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.

HYDROCARBON CONVERSION CATALYST.

Extremely low acidity ultrastable Y zeolite catalyst composition and process

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

一种按原料性质的双区串联多级协控催化裂解的方法

本发明提供一种按原料性质的双区串联多级协控催化裂解的方法，包括：原料包括富含烷烃的第一原料和富含烯烃的第二原料，采用包括依次串联的第一提升管、第二提升管的反应装置，使第一原料进入第一提升管与催化剂接触发生第一催化裂解反应；来自第一提升管的第一催化裂解产物和第一待生催化剂，以及第二原料进入第二提升管发生第二催化裂解反应；对第二催化裂解反应的产物实施气固分离后分别得到油气产物和待生催化剂；待生催化剂经汽提处理后进入再生器实施再生处理后，返回参与各催化裂解反应。本发明根据各类烃原料的裂解特点，对裂解工艺调整，使不同类型轻质烃原料利用一个系统被裂解，实现高收率轻烯烃的生产。

Catalytic reduction of NOx with high activity catalysts with NH3 reductant

Methods and systems for selective catalytic reduction of NOx with an ammonia reductant and a zeolite catalyst loaded with at least two metals selected from the group of tungsten, cobalt, and vanadium. An exhaust stream including NOx and a reductant stream including ammonia are provided to a catalytic reactor having the metal loaded zeolite catalyst at suitable operating temperatures for NOx reduction of at least 90%.

烯烃裂解催化剂及其制备方法和烯烃裂解方法

本发明提供了一种烯烃裂解催化剂及其制备方法和烯烃裂解方法，该催化剂的制备步骤包括：按照0‑30:50‑80:0‑30:0‑50质量比例混合经预处理的SAPO‑34、ZSM‑5、β和USY分子筛的至少两种得到复合分子筛，制成至少包括两种分子筛的复合分子筛，其中，所述预处理为：ZSM‑5分子筛、β分子筛和USY分子筛分别经阳离子交换处理；对复合分子筛依次进行非金属和金属改性，与基质和粘结剂混合打浆得到所述烯烃裂解催化剂。本发明的催化剂使用多孔道结构的复合分子筛并经多重改性处理，具有适宜的孔道结构和酸分布，实现对烯烃裂解反应路径的调控，烯烃的转化率和乙、丙烯的收率都得到提升，同时催化剂的寿命也得到提高。

Catalyst carrier with high diesel selectivity

본 발명은 (a) 하나 이상의 3가 금속 원소, 4가 금속 원소 및 2가 금속 원소의 산화물을 포함하는 담체 조성물의 전체 중량에 기초하여 적어도 30 중량%의 합성 분해 성분을 포함하는 담체 조성물에 관한 것이고, 상기 분해 성분은 평균 직경 1 ㎛이하 및 스택당 쌓는 소판의 평균 양이 20 이하인 기본 클레이 소판 및/또한 나트륨 및 칼륨의 전체 함량이 1 중량%이하이고 코겔의 전체 중량에 기초하여 사포나이트 성분 C A 이 60%이하인 코겔 및 (b) 담체 조성물의 전체 중량에 기초하여 단위 셀 크기가 24.35 Å이하인 1 - 25 중량%의 제올라이트 Y를 포함한다. 본 발명은 추가로 상기 담체 조성물 및 적어도 수소화 금속을 포함하는 촉매 및 상기 촉매를 사용하여 진한 원료를 중간 증류물로 전환하는 방법에 관한 것이다. The present invention relates to a carrier composition comprising (a) at least 30% by weight of a synthetic decomposition component based on the total weight of the carrier composition comprising at least one trivalent metal element, a tetravalent metal element and an oxide of a divalent metal element. The decomposition component is a basic clay platelet having an average diameter of 1 μm or less and an average amount of platelets stacked per stack of 20 or less and / or a total content of sodium and potassium of 1% by weight or less based on the total weight of the cogel and the saponite component Cogels having a C A of 60% or less and (b) 1-25% by weight zeolite Y having a unit cell size of 24.35 mm 3 or less based on the total weight of the carrier composition. The invention further relates to a catalyst comprising said carrier composition and at least a metal hydride and a process for converting a thick stock into an intermediate distillate using said catalyst.

具有高柴油选择性的催化剂载体

本发明涉及一种载体组合物，它含有(a)按载体组合物的总重计，至少30%(重量)合成的裂化组分，它包括一种或多种三价金属元素、四价金属元素和二价金属元素的氧化化合物，所述的裂化组分包括平均直径为1微米或更小以及平均重叠度为20片/叠或更小的基本白土片状物，和/或包括皂石含量C A 小于60%的共凝胶，按共凝胶的总重计，钠和钾的总量小于1%(重量)，以及(b)按载体组合物的总重计，1-25%(重量)单元晶胞尺寸小于24.35埃的Y型沸石。本发明还涉及一种含有所述的载体组合物和至少一种加氢金属的催化剂以及一种用所述催化剂将重质原料转化成中间馏分油的方法。

Highly selective catalyst for producing high-quality gasoline fractions from synthesis gas and method for production thereof

FIELD: chemistry. SUBSTANCE: invention relates to a catalyst for selective synthesis of high-quality gasoline fractions from synthesis gas and a method for production thereof. Described is a highly selective catalyst for producing high-quality gasoline fractions from synthesis gas, which consists of cobalt, a promoter and a molecular sieve, wherein the weight content of cobalt is 1-30%, the weight content of the promoter is 0.01-5%, and the remaining part is a molecular sieve, with respect to the weight of the catalyst, wherein the molecular sieve is one or more molecular sieves selected from molecular sieves Beta, ZSM-5, MOR, Y and MCM-22, wherein acidity of the molecular sieve is expressed through the amount of adsorbed NH 3 , and the adsorption capacity of the molecular sieve ranges from 0.16 to 0.50 mmol NH 3 /g; the molecular sieve has a microporous-mesoporous structure, wherein the micropores have diameter of 0.4-0.9 nm, and the mesopores have diameter of 2-30 nm, the specific surface area of the molecular sieve is 100-900 m 2 /g and the volume of micropores and mesopores is 0.1-0.6 cm 3 /g, respectively. Described is a method of producing a highly selective catalyst used for synthesis of high-quality gasoline fractions from synthesis gas by Fischer-Tropsch synthesis, involving the following steps: (1) preparing a weighed portion of a cobalt salt according to content of components given above, mixing with a solvent which is deionised water, alcohol or a ketone, to obtain a solution which contains a cobalt salt with concentration of 0.5-20 wt %; (2) preparing a weighed portion of a promoter according to content of components established above, adding to the prepared solution a cobalt salt and stirring for 0.5-3 hours; (3) preparing a weighed portion of a molecular sieve according to content of components established above, adding the molecular sieve to the prepared solution of cobalt salt, stirring for 0.1-15 hours and holding for 0.1-24 hours; (4) evaporating ...

一种润滑油基础油的生产方法

本发明公开了一种润滑油基础油的生产方法。该方法是采用加氢裂化和补充精制工艺，过程如下：在加氢裂化催化剂存在下，加氢裂化原料进行加氢裂化反应，所得的加氢裂化产物进行分离，得到加氢裂化尾油，加氢裂化尾油经补充精制，得到润滑油基础油；所述加氢裂化采用单段工艺流程或一段串联工艺流程，优选一段串联工艺流程，所述一段串联工艺流程为在加氢裂化催化剂之前装填加氢精制催化剂。该方法所制备的加氢尾油具有倾点更低和产率高等特点，可直接精制生产倾点更低，稳定性更好的润滑油基础油。

按原料类型的多区分区耦合床层控制多级催化裂解的方法

本发明提供一种按原料类型的多区分区耦合床层控制多级催化裂解的方法，原料包括含C4烃的第一原料、含C5‑C6烃的第二原料以及含C7‑C8烃的第三原料，采用包括第一下行管、第二下行管、提升管的反应装置，方法包括：第一原料进入第一下行管发生第一催化裂解反应；第二原料进入第二下行管发生第二催化裂解反应；第一催化裂解反应的产物、第二催化裂解反应的产物以及第三原料进入提升管发生第三催化裂解反应；对第三催化裂解反应的产物气固分离得到油气产物和待生催化剂；待生催化剂经汽提并再生后返回各催化裂解反应。本发明根据各类烃原料的裂解特点，使不同轻烃原料在不同的条件下利用一个系统被裂解，实现轻烯烃的高收率。

一种纤维素类生物质原料水相催化转化选择性制备c5-c6液态烷烃的方法

本发明公开了一种纤维素类生物质原料水相催化转化选择性制备C5‑C6液态烷烃的方法。一种纤维素类生物质原料水相催化转化选择性制备C5‑C6液态烷烃的方法，以铱基双金属催化剂复合分子筛催化剂作为催化剂，将生物质原料或纤维素加入水或含水溶剂中催化转化为C5‑C6液态烷烃。本发明以生物质原料为底物，避免了使用化石基产品，不仅有效实现了农林有机固废资源的有效利用，同时也减轻了环境问题，绿色可持续，生物质基原料转化率较高，反应完全，反应所使用的铱基双金属催化剂可循环使用，在该方法下，也可获得较高的C5‑C6液态烷烃产率。

Modified Y-type molecular sieve and manufacturing method, hydrocracking catalyst and manufacturing method, and hydrocarbon oil hydrocracking method

본 발명은 개질 Y형 분자체 및 그 제작법, 수첨분해 촉매 및 그 제작 방법, 그리고 탄화수소 오일 수첨 분해법을 개시하였다. 개질 Y형 분자체의 총량을 기준으로, 개질 Y형 분자체는 0.5-2 중량%의 Na 2 O를 함유하고, 개질 Y형 분자체의 적외선을 이용하는 피리딘 산 총량과 개질 Y형 분자체의 적외선을 이용하는 n-부틸피리딘 산 총량의 비율은 1-1.2이며, 개질 Y형 분자체의 적외선을 이용하는 피리딘 산 총량은 0.1-1.2mmol/g이다. 개질 Y형 분자체의 분자체 산성 중심부위는 대공극 채널 내에 집중적으로 분포되고, 해당 분자체를 왁스오일 수첨분해 반응 과정에 사용함으로써, 왁스오일중 대분자 환상 탄화수소계 물질의 반응 선택성의 향상에 유리하고, 2차 분해반응의 발생을 줄여주며, 수첨분해 테일오일의 품질을 개선시켜주고, 반응액의 제품수율을 향상시켜준다. The present invention discloses a modified Y-type molecular sieve and a method for preparing the same, a hydrocracking catalyst and a method for preparing the same, and a hydrocracking method for hydrocarbon oil. Based on the total amount of the modified Y-type molecular sieve, the modified Y-type molecular sieve contains 0.5-2% by weight of Na 2 O, the total amount of pyridine acid using infrared rays of the modified Y-type molecular sieve and the infrared rays of the modified Y-type molecular sieve The ratio of the total amount of n-butylpyridic acid using is 1-1.2, and the total amount of pyridine acid using infrared rays of the modified Y-type molecular sieve is 0.1-1.2 mmol/g. The acidic central region of the molecular sieve of the modified Y-type molecular sieve is intensively distributed in the macropore channels, and by using the molecular sieve in the wax oil hydrocracking reaction process, it is advantageous to improve the reaction selectivity of large molecular cyclic hydrocarbon-based substances in wax oil. It reduces the occurrence of secondary decomposition reaction, improves the quality of hydrocracked tail oil, and improves the product yield of the reaction solution.

生产羟基乙酸的方法

从一氧化碳和甲醛生产羟基乙酸的方法，利用包括包封在沸石的孔之内的酸性多金属氧酸盐化合物的催化剂，其中该沸石具有比该酸性多金属氧酸盐化合物大的笼，该沸石还具有其直径比该酸性多金属氧酸盐化合物小的孔。

Na-Y Molecular Sieve, H-Y Molecular Sieve, and Preparation Methods Thereof, Hydrocracking Catalyst, and Hydrocracking Method

본 발명은 Na-Y 분자체와 Na-Y 분자체의 제조방법, H-Y 분자체와 H-Y 분자체의 제조방법, 및 수소첨가분해 촉매(hydrocracking catalyst)와 수소첨가분해 방법을 개시한다. 상기 Na-Y분자체의 평균 입자 직경이 2~5μm이고, 1-10nm의 직경을 가진 공극들의 공극 부피의 합이 Na-Y 분자체의 총 공극 부피의 70~90%를 차지한다. 큰 입자 Na-Y 분자체로부터 얻은 H-Y 분자체는 수소첨가분해 촉매에서 산성 성분(acidic component)으로써 사용될 수 있다. H-Y 분자체를 포함한 수소첨가분해 촉매가 고분자를 포함하는 중유의 수소첨가분해 반응에 적용되었을 때, 이것은 수소첨가분해 반응에서 더 나은 분해 활성과 제품 생산성을 제공할 수 있다. The present invention discloses a method for producing Na-Y molecular sieve and Na-Y molecular sieve, a method for producing H-Y molecular sieve and H-Y molecular sieve, and a hydrocracking catalyst and a hydrogenolysis method. The average particle diameter of the Na-Y molecular sieve is 2 to 5 μm and the sum of the pore volumes of the pores with diameters of 1 to 10 nm accounts for 70 to 90% of the total pore volume of the Na-Y molecular sieve. The H-Y molecular sieve obtained from the large particle Na-Y molecular sieve can be used as an acidic component in the hydrocracking catalyst. When hydrocracking catalysts containing H-Y molecular sieves are applied to the hydrocracking of heavy oils containing polymers, this can provide better degradation activity and product productivity in hydrocracking reactions.

加氢裂化催化剂载体及其制备方法与应用

本发明提供了一种加氢裂化催化剂载体及其制备方法与应用。该加氢裂化催化剂载体是由氟硅酸铵改性的Y型沸石/氧化铝复合材料制得的，所述氟硅酸铵改性的Y型沸石/氧化铝复合材料是通过活性氧化铝、导向剂、硅源和水经过混合、水热晶化、氟硅酸铵改性制备得到的。本发明还提供了上述加氢裂化催化剂载体的制备方法。本发明进一步提供了上述加氢裂化催化剂载体在重油加氢裂化中的应用。本发明提供的加氢裂化催化剂载体适用于处理大分子、重油品的原料，在提高大分子转化几率等方面表现出优越的性能，能够提升加氢裂化催化剂的水平。

一种加氢裂化催化剂的制备方法

本发明公开了一种加氢裂化催化剂的制备方法。该方法包括如下步骤：（l）将第一载体组分加水打浆，得到浆液；（2）将含第一加氢活性金属组分的溶液和特定的有机化合物溶液分别或同时加入到所述浆液中，搅拌均匀；（3）将步骤（2）所得的物料进行过滤、洗涤、干燥，得到催化剂中间体；（4）在所述催化剂中间体中加入含有裂化酸性组分的第二载体组分进行混捏，经成型和干燥，得到催化剂成型体；（5）将含有第二加氢活性金属组分的浸渍液浸渍在所述催化剂成型体上，然后进行干燥，在惰性气体的保护下焙烧，得到所述的加氢裂化催化剂。该制备方法解决了硫化过程中温升过快的问题，且催化剂具有很好的加氢性能。