СЕЛЕКТИВНОЕ ПОЛУЧЕНИЕ ПАРА-КСИЛОЛА ПОСРЕДСТВОМ МЕТИЛИРОВАНИЯ ТОЛУОЛА

Изобретение относится к способу селективного получения параксилола, который включает взаимодействие толуола с метанолом в присутствии катализатора, содержащего пористый кристаллический алюмосиликатный цеолит, имеющий параметр диффузии по 2,2-диметилбутану примерно 0,1-15 с-1, измеренный при температуре 120oС и давлении 2,2-диметилбутана (8 кПа). Пористый кристаллический материал предпочтительно представляет собой цеолит со средним размером пор, в частности ZSM-5, который подвергают обработке водяным паром в жестких условиях при температуре, по меньшей мере, 1000oС. Алюмосиликатный цеолитный катализатор предпочтительно объединяют с, по меньшей мере, одним оксидным модификатором, предпочтительно содержащим фосфор, чтобы регулировать снижение объема микропор материала в ходе стадии обработки паром. Технический результат - увеличение выхода продукта, упрощение технологии процесса. 2 с. и 15 з.п. ф-лы, 10 табл., 3 ил.

Способ получения пропиленоксида

Изобретение относится к непрерывному способу получения пропиленоксида. Предложенный способ включает: (i) предоставление жидкого потока поступающего материала, содержащего пропен, перекись водорода, ацетонитрил, воду, необязательно пропан и, по меньшей мере, одну растворенную калиевую соль оксикислоты фосфора; (ii) подачу жидкого потока поступающего материала, предоставленного на стадии (i), в реактор эпоксидирования, содержащий катализатор, содержащий титановый цеолит структурного типа MWW, содержащий цинк, и воздействие на жидкий поток поступающего материала условий реакции эпоксидирования в реакторе эпоксидирования с получением реакционной смеси, содержащей пропиленоксид, ацетонитрил, воду, по меньшей мере, одну растворенную калиевую соль оксикислоты фосфора, необязательно пропен и необязательно пропан; (iii) удаление отходящего потока из реактора эпоксидирования, причем отходящий поток содержит пропиленоксид, ацетонитрил, воду, по меньшей мере, часть, по меньшей мере, одной растворенной ...

КАТАЛИЗАТОР ДЛЯ ПОЛУЧЕНИЯ БИСФЕНОЛОВ

Изобретение относится к способу получения катализатора для получения бисфенолов. Способ получения катализатора для получения бисфенолов, содержащего кислотную катионообменную смолу, на которую адсорбируют серосодержащее соединение амина, включает стадии введения кислотной катионообменной смолы в контакт с кислотными сточными водами, содержащими серосодержащее соединение амина, выпускаемыми со стадии получения катализатора, при этом сточные воды имеют начальную концентрацию указанного серосодержащего соединения амина, равную 170 ч./млн (мас.) и менее и контакт циркуляцией осуществляют до уменьшения его концентрации до 5 ч./млн (мас.) или менее. Технический результат заключается в значительном удалении серосодержащего соединения амина из сточных вод и упрощении переработки сточных вод после получения катализатора. 2 з.п. ф-лы.

ЦЕОЛИТСОДЕРЖАЩИЙ КАТАЛИЗАТОР, СПОСОБ ЕГО ПОЛУЧЕНИЯ И СПОСОБ ПРЕВРАЩЕНИЯ АЛИФАТИЧЕСКИХ УГЛЕВОДОРОДОВ В КОНЦЕНТРАТ АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ ИЛИ ВЫСОКООКТАНОВЫЙ КОМПОНЕНТ БЕНЗИНА (ВАРИАНТЫ)

Изобретение относится к нефтеперерабатывающей и нефтехимической промышленности и посвящено созданию катализаторов, используемых в переработке алифатических углеводородов в концентрат ароматических углеводородов или высокооктановый компонент бензина. Описан цеолитсодержащий катализатор, который содержит цеолит группы пентасила с силикатным модулем SiO2/Al2О3=55-102 моль/моль и остаточным содержанием оксида натрия 0,02-0,07 мас.% и оксиды цинка, олова и лантана в качестве элементов структуры цеолита, а в качестве промотора - оксид хрома при следующем содержании компонентов, мас.%: цеолит 65,0-80,0, ZnO 0,0-4,0, Zi2O3 0,0-0,8, SnO2 0,0-2,5, Cr2O3 0,0-5,0, Na2O 0,02-0,07, связующий компонент - остальное. Описан способ получения цеолитсодержащего катализатора, включающий гидротермальный синтез Na-формы цеолита с последующим солевым ионным обменом и получением аммонийной формы цеолита, после чего аммонийную форму цеолита модифицируют лантаном, в модифицированную лантаном аммонийную форму цеолита ...

ФОСФОРСОДЕРЖАЩИЙ КАТАЛИЗАТОР ДЛЯ ПРЕВРАЩЕНИЯ ОКСИГЕНАТОВ В ОЛЕФИНЫ

Изобретение относится к способу приготовления фосфорсодержащего катализатора, включающему следующие стадии: (a) экструдирование смеси, которая содержит цеолит и оксид алюминия или гидрат оксида алюминия, в качестве связующего, (b) кальцинирование полученного на стадии (а) экструдата, (c) обработка полученного на стадии (b) кальцинированного экструдата водяным паром, (d) нанесение фосфорсодержащего соединения на обработанный водяным паром экструдат со стадии (с) и (e) кальцинирование модифицированного фосфором экструдата со стадии (d), причем массовая доля фосфора в полученном после стадии (е) катализаторе составляет от 0,8 до 2,5 мас. %. Также изобретение относится к катализатору превращения оксигенатов в олефины, способу получения олефинов из оксигенатов и применению катализатора для превращения оксигенатов в олефины. Получаемый катализатор обладает увеличенным сроком службы при остающейся неизменно селективности и увеличенной степени превращения. 4 н. и 14 з.п. ф-лы, 7 ил., 2 табл., 7 ...

Фотокатализатор и способ его получения

Изобретение относится к технологии получения и использования в производстве фотокатализаторов для разложения органических веществ и загрязнителей при очистке воды, воздуха и в других фотохимических процессах, в газовых и оптических сенсорах. Предлагаемый фотокатализатор содержит матрицу на основе аморфного диоксида кремния и равномерно распределенный в матрице активный компонент, в качестве которого фотокатализатор содержит гидроксосиликат кобальта состава Co3(Si2O5)2(OH)2. При этом соотношение компонентов в фотокатализаторе составляет, мас.%: гидроксосиликат кобальта - 0,2-3,0; аморфный диоксид кремния - 97,0-99,8. Также изобретение относится к способу получения предлагаемого фотокатализатора. Технический результат - разработка состава фотокатализатора для разложения органических соединений, обеспечивающего расширение номенклатуры используемых в настоящее время фотокатализаторов, при этом фотокатализатор может быть получен технологически простым и надежным способом. 2 н.п. ф-лы, 3 ил., ...

КРИСТАЛЛИЧЕСКИЙ ОКСИГИДРОКСИД-МОЛИБДОВОЛЬФРАМАТ ПЕРЕХОДНОГО МЕТАЛЛА

Разработан активный катализатор гидрообработки, предназначенный для использования в процессах конверсии углеводородов: гидроденитрификации, гидрообессеривания, гидродеметаллирования, гидродесиликации, гидродеароматизации, гидроизомеризации, гидроочистки, гидрофайнинга и гидрокрекинга. Катализатор представляет собой материал кристаллического оксигидроксида-молибдовольфрамата металла, имеющего формулу:(NH)M(OH)MoWO,где а находится в диапазоне от 0,1 до 10; М представляет собой металл, выбранный из Mg, Mn, Fe, Co, Ni, Cu, Zn и их смесей; b находится в диапазоне от 0,1 до 2; х находится в диапазоне от 0,5 до 1,5; у находится в диапазоне от 0,01 до 0,4; где сумма (x+y) должна быть ≤1,501; z представляет собой число, которое соответствует сумме валентностей а, M, b, x и y; при этом материал имеет порошковую рентгендифрактограмму, показывающую пики при d-расстояниях, перечисленных в таблице A:Таблица А3 н. и 7 з.п. ф-лы, 1 ил., 1 табл., 3 пр.

СПОСОБ ПОЛУЧЕНИЯ ФЕНОЛА ИЛИ ЕГО ПРОИЗВОДНЫХ

Использование: окислительное гидроксилирование бензола или других ароматических соединений с получением фенола или его производных. Сущность изобретения: фенол или его производные получают газофазным окислительным гидроксилированием бензола или его производных закисью азота при температуре 225-450oС в присутствии предварительно активированного цеолитного катализатора. Активацию ведут при температуре 350-950oC водяным паром или смесью водяного пара с газом-разбавителем при концентрации водяного пара в смеси 3-100% мол. Предпочтительно в качестве разбавителя используют воздух, диоксид углерода, кислород, инертный газ или их смесь. 1 з.п.ф-лы, 4 табл.

Способ приготовления катализаторов для получения синтез-газа путем углекислотной конверсии метана

Изобретение относится к области химии, нефтехимии и нефтепереработки, в частности, к способу приготовления катализаторов для получения синтез-газа реакцией углекислотной конверсии метана. Способ приготовления катализатора заключается в растворении солей-предшественников, добавлении комплексообразователя, выпаривании раствора, прокаливании в муфельной печи, при этом в качестве дополнительной соли-предшественника используют нитрат кобальта Co(NO)⋅3HO, перед добавлением комплексообразователя соли-предшественники Gd(NO)⋅6HO, Fe(NO)⋅9HO, Co(NO)⋅3HO, взятые в мольном соотношении 1:х:(1-х), где х=0-0.9, растворяют в деионизированной воде, в качестве комплексообразователя используют лимонную кислоту, взятую в весовом соотношении к смеси нитратов от 2:1 до 2.5:1, после полного растворения лимонной кислоты добавляют раствор аммиака до установления рН от 6 до 6.5, а полученный после выпаривания порошок прокаливают при 450°С в течение 2 ч и 1-2 ч при температуре 600-800°С. Технический результат заключается ...

МИКРОСФЕРИЧЕСКИЙ КАТАЛИЗАТОР ДЛЯ КРЕКИНГА НЕФТЯНЫХ ФРАКЦИЙ И СПОСОБ ЕГО ПРИГОТОВЛЕНИЯ

Изобретение относится к области нефтеперерабатывающей промышленности, а именно к катализатору крекинга нефтяных фракций и способу его приготовления. Описан микросферический катализатор для крекинга нефтяных фракций, который содержит ультрастабильный цеолит Y в катион-декатионированной форме с решеточным модулем 5,2-6,0, содержащий 1,0-1,5 мас.% оксида натрия, 10-14 мас.% оксидов редкоземельных элементов, и/или ультрастабильный цеолит с решеточным модулем 6,0-10,0, содержащий 0,5-1,0 мас.% оксида натрия, 7-10 мас.% оксидов редкоземельных элементов и матрицу, в качестве компонентов которой используют аморфный алюмосиликат, гидроксид алюминия и бентонитовую глину, при следующем соотношении компонентов, мас.%: цеолит Y или смесь цеолитов Y 15-30, аморфный алюмосиликат 20-45, гидроксид алюминия 10-40, бентонитовая глина 10-40. Способ приготовления описанного выше катализатора включает проведение ионных обменов на катионы редкоземельных элементов и аммония на цеолите NaY, ультрастабилизацию цеолита ...

МОДИФИЦИРОВАННОЕ ФОСФОРОМ МОЛЕКУЛЯРНОЕ СИТО СО СТРУКТУРОЙ MFI, ВСПОМОГАТЕЛЬНОЕ СРЕДСТВО ДЛЯ КАТАЛИТИЧЕСКОГО КРЕКИНГА И КАТАЛИЗАТОР КАТАЛИТИЧЕСКОГО КРЕКИНГА, СОДЕРЖАЩИЕ МОДИФИЦИРОВАННЫЕ ФОСФОРОМ МОЛЕКУЛЯРНЫЕ СИТА СО СТРУКТУРОЙ MFI, А ТАКЖЕ ПРОЦЕССЫ ДЛЯ ИХ ПРИГОТОВЛЕНИЯ

Настоящее изобретение относится к модифицированному фосфором молекулярному ситу со структурой MFI. Описаны модифицированное фосфором молекулярное сито со структурой MFI, имеющее значение K, удовлетворяющее условию 70%≤K≤90%, где K=P1/P2×100%, P1 представляет собой измеренное способом XPS массовое содержание фосфора в области с площадью 100 кв.нм и вертикальной глубиной от 0 до 2 нм на любой поверхности кристаллического зерна молекулярного сита, P2 представляет собой измеренное способом EPMA массовое содержание фосфора в области с площадью 100 кв.нм и вертикальной глубиной от 5 до 10 нм на любой поверхности кристаллического зерна молекулярного сита, и способ его получения. Также описаны вспомогательное средство для каталитического крекинга, которое, в расчете на сухую массу вспомогательного средства для каталитического крекинга, содержит 5-75 мас.% указанного модифицированного фосфором молекулярного сита со структурой MFI, 1-40 мас.% связующего вещества и 0-65 мас.% второй глины, способ ...

Катализатор для получения акриловой кислоты и ее производных на основе биологического сырья и способ его получения

СПОСОБ АКТИВАЦИИ КАТАЛИЗАТОРА ДЛЯ ДЕГИДРИРОВАНИЯ Н-БУТЕНА

Способ активации катализатора для дегидрирования н-бутена путем обработки катализатора водяным паром при повышенной температуре, отличающийся тем, что, с целью повышения активности катализатора, обработку проводят при 800-820oC в течение 30-60 мин при содержании кислорода в водяном паре 0,05-0,10 мол.%.

СПОСОБ ПОЛУЧЕНИЯ УГЛЕРОДНОГО НОСИТЕЛЯ ДЛЯ КАТАЛИЗАТОРА

Изобретение относится к каталитической химии, в частности к получению углеродного носителя для катализатора. Цель - получение носителя, обеспечивающего увеличенные активности и механическую прочность катализатора. Получение носителя ведут обработкой сажи газообразной углеводородной смесью, затем пароводушной смесью с последующей дополнительной обработкой углеродного материала газообразными углеводородами до увеличения его массы на 1 - 50%. Активность катализатора (приготовленного пропиткой гранулированного углеродного носителя смесью растворов палладийхлористоводородной кислоты и карбоната натрия с последующим восстановлением водородом) при гидрировании 1 моль С6H6 78 г-ат Рd•c•10-2 при механической прочности на раздавливание 194 кг/см2. 1 табл.

КАТАЛИЗАТОРЫ SCR С УЛУЧШЕННОЙ НИЗКОТЕМПЕРАТУРНОЙ ЭФФЕКТИВНОСТЬЮ И СПОСОБЫ ИХ СОЗДАНИЯ И ИСПОЛЬЗОВАНИЯ

METHOD OF PREPARING CATALYST FOR ACETIC ACID GAS-PHASE SYNTHESIS

Способ приготовления катализатора для газофазного синтеза уксусной кислоты

Сущность изобретения: продукт-катализатор (КТ) - борофосфатный комплекс на активированном угле получают обработкой угля перегретым водяным паром при 105- 140° С в течение 1-7 мин с последующим погружением обработанного угля в раствор борофосфатного комплекса, имеющий температуру окружающей среды, выдерживанием в течение 4-10 мин, удалением избытка раствора фильтрацией и термообработкой . Характеристика КТ: повышенная активность. 1 табл., 1 ил.

Способ активирования медно-хромового катализатора для гидрирования @ , @ -ненасыщенных альдегидов

Способ получения катализаторов

Способ активации глиноземного или кремнеземно-глиноземного катализатора

Katalysator, Verfahren zur Herstellung desselben und Anwendung zur Herstellung von tertiären Olefinen aus Alkyl-Tert-Alkyl-Äthern.

Fester kristalliner Phosphorsäure-Katalysator für die Umwandlung von Kohlenwasserstoffen

METHOD OF PREPARING CRYSTALLINE ZEOLITE CATALYST OF HIGH ACTIVITY

Verfahren zur Herstellung von geträgertem Ruthenium auf siliciumdioxid-modifiziertem Titandioxid, und Verfahren zur Herstellung von Chlor

Eine Aufgabe der Erfindung ist es, ein Verfahren zur Herstellung eines geträgerten Rutheniumoxids bereitzustellen, wobei Siliciumdioxid effektiv auf einen Titandioxid-Träger geträgert werden kann, und ein geträgertes Rutheniumoxid mit überlegener thermischer Stabilität und Lebensdauer des Katalysators erhalten wird. Eine andere Aufgabe der vorliegenden Erfindung ist es, ein Verfahren zur stabilen Herstellung von Chlor für einen längeren Zeitraum unter Verwendung des geträgerten Rutheniumoxids, das mit dem vorstehend beschriebenen Verfahren erhalten wurde, bereitzustellen. Die Erfindung betrifft ein Verfahren zur Herstellung eines geträgerten Rutheniumoxids, in dem Rutheniumoxid und Siliciumdioxid auf einen Titandioxid-Träger geträgert werden, wobei ein Titandioxid-Träger mit einer Alkoxysilanverbindung in Kontakt gebracht wird, gefolgt von Trocknen unter einem Strom Wasserdampf enthaltenden Gases, dann einem ersten Kalzinieren unter einer Atmosphäre eines oxidierenden Gases unterzogen wird ...

KATALYSATOR ZUR UMWANDLUNG VON KOHLENWASSERSTOFFVERBINDUNGEN UND VERFAHREN ZUR SELEKTIVEN HERSTELLUNG VON MITTELOELEN.

Geformte Sulfonatgruppen-haltige Organopolysiloxane, Verfahren zu ihrer Herstellung und Verwendung

SOLID CATALYST FOR HETEROGENEOUS REACTIONS

... 1447707 Acidic catalyst composition IMI (TAMI) INSTITUTE FOR RESEARCH & DEVELOPMENT 15 Jan 1974 [17 Jan 1973] 01838/74 Heading B1E [Also in Divisions C2 and C5] A catalyst comprises a solid carrier and carboxymethane sulphonic acid and/or products resulting from thermal treatment thereof at a temperature not exceeding 330‹C. The catalyst is formed by impregnating the carrier with the acid or precursors thereof (e.g. glacial acetic acid and sulphur trioxide, acetic acid anhydride and sulphuric acid, acetic acid and oleum or acetylsulphuric acid), drying, if desired under reduced pressure, at a temperature not exceeding 170‹C, then baking at 170-330‹C to constant weight. The carrier may be an inorganic oxide, an acid based on such an oxide or a salt thereof, e.g. alumina, silica, bona, zirconia, silica-alumina, silica-alumina-zirconia, diatomaceous earth, atterpulgus clay or bentonite or may be active carbon or graphite. The carrier may be pretreated with an acid before the impregnation.

SURFACE ALUMINA

... 1492273 Surface modified aluminium oxide SNAMPROGETTI SpA 28 Oct 1974 [19 Sept 1974] 46610/74 Heading ClA Surface modified aluminium oxide, which after dehydration has an ir spectra with a band at 3745 cm.-1 characteristic of the Si-OH group and the bands at 3795 and 3737 cm.-1 normally attributable to -OH groups on the oxide surface are absent and the band at 3698 cm.-1 reduced, is prepared by impregnation of the oxide with an organo-silicon compound containing hydrolysable radicals bound to silicon and thence subjecting the material free from unreacted impregnating material and any volatile reaction products to hydrolysis with steam to hydrolyse the hydrolysable radicals bound via silicon to the aluminium oxide. The hydrolysis can be effected at room temperature to 500‹ C. and the silicon compound selected from methyl orthosilicate, ethyl orthosilicate, n-propyl orthosilicate, isopropyl orthosilicate, n-butyl orthosilicate, sec-butyl orthosilicate, iso-butyl ...

PROCEDURE FOR REMOVING FROM HALOGENS FROM NON ZEOLITI MOLECULAR SIEVE CATALYSTS

ZEOLITHI MATERIAL OF PENTASIL STRUKTURTYP, ITS PRODUCTION AND ITS USE

IRREGULARLY FIGURATIONS, NOT SPHERICAL ONES CARRIER CATALYST AND PROCEDURE FOR THE HYDROGENATING CONVERSION OF HEAVY ERDÖLFRAKTIONEN

PROCEDURE FOR THE PRODUCTION OF ALUMINA USABLE AS CATALYST CARRIER

PRODUCTION OF A MOL FILTER CATALYST COMPOSITION AND A USE WITH PROCESSES OF CONVERSION

PROCEDURE FOR THE TREATMENT OF STRONG-SOUR CATION EXCHANGER CATALYSTS.

CATALYST, PROCEDURE FOR THE PRODUCTION THE SAME AND APPLICATION FOR THE PRODUCTION OF TERTIARY OLEFINEN FROM ALKYL TERT ALKYL ETHERS.

PROCEDURE FOR THE PRODUCTION OF ALUMINA USABLE AS KATALYSATORTRAGER

FAT BED PROCEDURE FOR THE SUESSEN OF ERDOELFRAKTIONEN.

CATALYST FOR THE CLEANING OF THE EXHAUST GASES FROM DIESEL ENGINES AND PROCEDURES TO ITS PRODUCTION

ENTALUMINIERTER KATALYSATORTRÄGER, PROCEDURE FOR the PRODUCTION of the KATALYSATORTRÄGERS AND PROCEDURE FOR HYDRATISIERUNG OF C2 OR C3-OLEFINEN WITH WATER IN PRESENCE of a CATALYST, WHICH EXISTS FROM THIS WITH ACID SOAKED KATALYSATORTRÄGER

DIMERIZATION OF OLEFINEN

MIDDLE DISTILLATE SELECTIVE HYDROCRACKING PROCESS

PROCESS FOR THE PREPARATION OF EPOXIDATION CATALYSTS

Fischer-Tropsch catalysts

A method of producing an alumina-supported cobalt catalyst for use in a Fischer-Tropsch synthesis reaction, which comprises: calcining an initial -alumina support material at a temperature to produce a modified alumina support material; impregnating the modified alumina support material with a source of cobalt; calcining the impregnated support material, activating the catalyst with a reducing gas, steam treating the activated catalyst, and activating the steam treated catalyst with a reducing gas.

Mixed metal oxide catalysts for propane and isobutane oxidation and ammoxidation, and methods of preparing same

Photocatalyst and method for production

The present invention relates generally to methods for producing modified titanium dioxide based photocatalysts via a sol-gel process. The present invention also relates to photocatalysts produced according to the methods of the invention and uses of the photocatalysts for the degradation of contaminants in samples.

STABILIZED ALUMINA

Process for producing light olefins

Multi-stage reforming process using rhenium-containing catalyst in the final stage

QUASI-CRYSTALLINE BOEHMITES CONTAINING ADDITIVES

The present invention pertains to a quasi-crystalline boehmite containing additive in a homogeneously dispersed state. Suitable additives are compounds containing elements selected from the group of alkaline earth metals, alkaline metals, transition metals, actinides, silicon, gallium, boron, titanium and phosphorus. Said QCBs according to the invention may be prepared in several ways. In general, a quasi-crystalline boehmite precursor and an additive are converted to a quasi-crystalline boehmite containing the additive in a homogeneously dispersed state. The application is also directed to shaped particles and catalysts comprising the quasi-crystalline boehmite to transition aluminas obtainable from these quasi-crystalline boehmites and to catalyst compositions comprising such transition alumina.

CATALYST COMPOSITIONS

PROCESS FOR THE PREPARATION OF A CATALYST

ODH CATALYST FORMULATIONS

The oxidative dehydrogenation of ethane comprises contacting a mixture of ethane and oxygen in an ODH reactor with an ODH catalyst under conditions that promote oxidation of ethane into ethylene. Conditions within the reactor are controlled by the operator and include, but are not limited to, parameters such as 5 temperature, pressure, and flow rate. Conditions will vary and can be optimized for a specific catalyst, or whether an inert diluent is used in the mixing of the reactants. Disclosed herein is a catalyst consisting of: Mo0-1W0.3-1V0.2-0.4Te0.06-0.10Fe0.0-0.10Nb0.08-0.18Ox where X is determined by the valance of the metals.

FLUID CATALYTIC CRACKING PROCESS

A STABILIZED TRANSITION ALUMINA CATALYST SUPPORT FROM BOEHMITE AND CATALYSTS MADE THEREFROM

This invention relates to methods for making a stabilized transition alumina of enhanced hydrothermal stability, which include the introduction of at least one structural stabilizer; a steaming step before or after the introduction step, wherein steaming is effective in transforming a transition alumina at least partially to boehmite and/or pseudoboehmite; and a calcining step to create a stabilized transition alumina. The combination of the structural stabilizer and the steaming step is believed to impart high hydrothermal stability to the alumina crystal lattice. Particularly preferred structural stabilizers include boron, cobalt, and zirconium. The stabilized transition alumina is useful as a catalyst support for high water partial pressure environments, and is particularly useful for making a catalyst having improved hydrothermal stability. The invention more specifically discloses Fischer- Tropsch catalysts and processes for the production of hydrocarbons from synthesis gas.

HYDROCARBON CONVERSION PROCESSES USING NON-ZEOLITIC MOLECULAR SIEVE CATALYSTS

Methods of removing halogen from non-zeolitic molecular sieve catalysts, the catalyst produced from such methods, and the use of such catalysts in hydrocarbon conversion processes. Several processes are disclosed allowing to remove most, if not all, of the halogen contained in the catalysts. The processes comprise steam-treating the catalyst at a temperature of from 400~C to 1000~C. The hydrocarbon conversion processes include the conversion of oxygenates to olefins, the conversion of oxygenates and ammonia to alkylamines, the conversion of oxygenates and aromatic compounds to alkylated aromatic compounds, cracking and dewaxing.

HYDROTREATING CATALYST AND PROCESS

METHOD AND CATALYST FOR PRODUCING HIGH OCTANE COMPONENTS

The group of inventions relates to a process of co-converting hydrocarbon feedstock with a high content of unsaturated hydrocarbons and aliphatic alcohols into components of high octane gasolines or aromatic hydrocarbons, as well as to catalysts of such a co-conversion. The method of co-converting hydrocarbon fractions and oxygenates into high octane components of fuels or aromatic hydrocarbons including contacting a hydrocarbon stream mixed with oxygenates with a catalyst under a reduced pressure and with heating. The process is carried under using a catalyst that contains the HZSM-5 zeolite that passed thermal and steam treatment.

MULTI-STAGE REFORMING PROCESS USING RHENIUM-CONTAINING CATALYST IN THE FINAL STAGE

This is a process for upgrading a petroleum naphtha fraction. The naphtha is subjected to reforming and the reformate is cascaded to a benzene and toluene synthesis zone over a benzene and toluene synthesis catalyst comprising a molecular sieve of low acid activity. The preferred molecular sieve is steamed ZSM-5. The benzene and toluene synthesis zone is operated under conditions compatible with the conditions of the reformer such as temperatures of above about 800 ~F (427 ~C). In one aspect of the invention, the benzene and toluene synthesis catalyst includes a metal hydrogenation component from group VII(B), specifically rhenium. In one mode of operation, the benzene and toluene synthesis catalyst replaces at least a portion of the catalyst in the reformer. The process produces a product containing an increased proportion of benzene, toluene, and/or xylenes, and a reduced portion of alkylated aromatics, as compared to reformate.

HYDROTHERMAL PRETREATMENT FOR INCREASING AVERAGE PORE SIZE IN CATALYST SUPPORTS

A pretreatment method for increasing the average pore size of a catalyst support is disclosed which increases the diffusivity and effectiveness factor .eta.. The pretreatment method includes calcining the support in moisturized air at an elevated temperature sufficient to increase the average pore size. In some embodiments, the support may be treated with an acidic/basic solution prior to the calcination step. Alternatively, the calcination step may occur in a gas mixture including water/air/acidic (or basic) gases.

NOVEL IM-21 ORGANIC-INORGANIC HYBRID SOLID AND PROCESS FOR PREPARING SAME

On décrit un nouveau solide hybride cristallisé à matrice mixte organique-inorganique présentant une structure tridimensionnelle contenant un réseau inorganique de centres métalliques à base de zinc connectés entre eux par des ligands organiques déprotonnés constitués par l'entité -02C-C6H2-(0)2-C02. Ce nouveau solide est appelé IM-21 et présente un diagramme de diffraction des rayons X tel que donné ci-dessous.

HEAVY HYDROCARBON OIL CRACKING CATALYST AND METHOD FOR CRACKING HEAVY HYDROCARBON OIL

Provided are a heavy hydrocarbon oil cracking catalyst having good activity and a heavy hydrocarbon oil cracking method using said catalyst, which enable efficient production of light hydrocarbon oil from heavy hydrocarbon oil without employing high pressure hydrogen gas. The heavy hydrocarbon oil cracking catalyst is used when heavy hydrocarbon oil is cracked in the presence of water, and contains a group 4A element at an amount of 10 mass% or more. The heavy hydrocarbon oil cracking method produces light hydrocarbon oil by bringing heavy hydrocarbon oil having a weight-average molecular weight of 500 or more into contact with the catalyst in the presence of water.

FISCHER-TROPSCH SYNTHESIS CATALYST, MANUFACTURING METHOD THEREFOR, AND HYDROCARBON MANUFACTURING METHOD

Disclosed is a Fischer-Tropsch synthesis catalyst in which metal atoms in the form of metallic cobalt and/or a cobalt oxide are supported by a silica-containing support. Said metallic cobalt and/or cobalt oxide constitutes between 10% and 30% of the mass of the catalyst. The mean pore diameter of the support is between 8 and 25 nm, and the mean crystallite diameter of the metallic cobalt and/or cobalt oxide is greater than or equal to the mean pore diameter of the support but less than 35 nm.

TREATMENT OF ARSINE REMOVAL CATALYSTS

HYDROCARBON CONVERSION

This is a process for upgrading a petroleum naphtha fraction. The naphtha (10) is subjected to reforming (16a, 16b, 16c) and the reformate is cascaded to a benzene and toluene synthesis zone (18) over a synthesis catalyst comprising a molecular sieve of low acid activity. The preferred molecular sieve is steamed ZSM-5. The benzene and toluene synthesis zone (18) is operated under conditions compatible with the conditions of the reformer such as pressures of above about 50 psig (446 kPa) and temperatures above about 800 ~F (427 ~C). In one aspect of the invention, the benzene and toluene synthesis catalyst includes a metal hydrogenation component such as cobalt, nickel, platinum and palladium. In one mode of operation, the benzene and toluene synthesis catalyst replaces at least a portion of the catalyst of the reformer. The process produces a product containing an increased proportion of benzene and toluene, and reduced proportion of C8 aromatics, particularly ethylbenzenes, as compared ...

Verfahren zur Durchführung katalytischer Reaktionen.

Verfahren zur Herstellung eines Oxyde des Vanadiums und Zinns enthaltenden Katalysators

PROCEDURE FOR THE TREATMENT OF STRONG-SOUR CATION EXCHANGER CATALYSTS.

METHOD OF PREPARING CATALYST BASED ON MOLECULAR SIEVE

ПРИМЕНЕНИЕ КАТАЛИЗАТОРА НА ОСНОВЕ МОДИФИЦИРОВАННОГО ФОСФОРОМ ЦЕОЛИТА В ПРОЦЕССЕ ДЕГИДРАТАЦИИ СПИРТОВ

В первом варианте реализации настоящее изобретение относится к применению катализатора для конвертации по меньшей мере одного спирта в лёгкие олефины в процессе дегидратации с получением олефина, имеющего одинаковое со спиртом число атомов углерода, при этом катализатор приготовлен на основе модифицированного фосфором цеолита способом, включающим следующие шаги в указанной последовательности: a) взять цеолит, в структуру которого входит хотя бы одно десятичленное кольцо, по усмотрению обработать цеолит паром; b) смешать цеолит, указанный в шаге a), как минимум с одним из связующих компонентов и структуронаправляющих агентов, после чего сформовать смесь; c) по усмотрению выполнить ионообмен; d) по усмотрению обработать паром сформованный катализатор, произвольно - перед шагом c), при этом по меньшей мере одна из указанных обработок паром на шаге d) и на шаге a) обязательна; e) ввести в катализатор по меньшей мере 0,1 мас.% фосфора, применяя сухую импрегнацию или парофазное химическое осаждение ...

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА, КАТАЛИЗАТОР, А ТАКЖЕ СПОСОБ ОКИСЛИТЕЛЬНОГО ДЕГИДРИРОВАНИЯ УГЛЕВОДОРОДОВ

Изобретение относится к способу получения катализатора, причем катализатор готовится в форме металлоксидного катализатора, который содержит по меньшей мере один элемент из группы Mo, Te, Nb, V, Cr, Dy, Ga, Sb, Ni, Co, Pt и Ce. Согласно изобретению предусмотрено, что катализатор K подвергают дополнительной обработке для повышения содержания фазы M1, причем катализатор K приводят в контакт с водяным паром при давлении ниже 100 бар и/или с кислородом с образованием дополнительно обработанного катализатора K'. Кроме того, изобретение относится к полученному этим способом катализатору K', а также к способу окислительного дегидрирования на катализаторе K' согласно изобретению.

CATALYST BASED ON MODIFIED PHOSPHORUS OF ZEOLITE WITH PARTIAL ALPO-STRUCTURE

КАТАЛИЗАТОРЫ ИЗ НАНОПРОВОЛОКИ И СПОСОБЫ ИХ ПРИМЕНЕНИЯ И ПОЛУЧЕНИЯ

Изобретение относится к каталитическому материалу для окислительного сочетания метана в форме прессованной таблетки, экструдата или монолитной структуры, содержащему совокупность каталитических нанопроволок, содержащих один или более легирующих элементов, и разбавитель или подложку, где разбавитель или подложка содержат одно или более соединений щелочно-земельного металла, а также к способу получения этана, этилена или их комбинации с использованием указанного каталитического материала.

КАТАЛИЗАТОРЫ ФИШЕРА-ТРОПША

Способ приготовления кобальтового катализатора на алюмооксидном носителе для использования в реакции синтеза Фишера-Тропша, который включает прокаливание исходного материала γ-алюмооксидного носителя при температуре, позволяющей получать материал модифицированного алюмооксидного носителя; пропитку материала модифицированного алюмооксидного носителя источником кобальта; прокаливание пропитанного материала носителя; активирование катализатора восстановительным газом; обработку активированного катализатора водяным паром и активирование обработанного водяным паром катализатора восстановительным газом.

НОСИТЕЛЬ КАТАЛИЗАТОРА, ОЧИЩЕННЫЙ ОТ АЛЮМИНИЯ, СПОСОБ ПОЛУЧЕНИЯ ЭТОГО НОСИТЕЛЯ КАТАЛИЗАТОРА И СПОСОБ ГИДРАТАЦИИ С2- ИЛИ С3-ОЛЕФИНОВ ВОДОЙ В ПРИСУТСТВИИ КАТАЛИЗАТОРА, ПРЕДСТАВЛЯЮЩЕГО СОБОЙ ЭТОТ НОСИТЕЛЬ, ПРОПИТАННЫЙ КИСЛОТОЙ

Изобретение относится к носителю катализатора, очищенному от алюминия, к способу получения носителя катализатора с пониженным содержанием алюминия на основе слоистых силикатных материалов, встречающихся в природе, например монтмориллонита, а также к способу гидратации С2- или С3-олефинов водой, при котором используют носитель катализатора с пониженным содержанием алюминия. Для реакции гидратации, катализируемой кислотой, носитель пропитывают фосфорной кислотой. Улучшение согласно изобретению по сравнению с обычными способами гидратации состоит в том, что не происходит выщелачивание алюминия из носителя в присутствии фосфорной кислоты. И, таким образом, при реакции не будет происходить блокирование фосфатом алюминия последовательно подсоединенных аппаратов. Международная заявка была опубликована вместе с отчетом о международном поиске.

MAINTENANCE OF CATALYTIC ACTIVITY MOLECULAR SIEVE IN CONDITIONS OF PRESENCE OF WATER STEAM

ПОРОШКОПОДІБНИЙ ДІОКСИД ТИТАНУ ТА СПОСІБ ЙОГО ОДЕРЖАННЯ ПОЛУМЕНЕВИМ ГІДРОЛІЗОМ

У заявці описаний одержаний полуменевим гідролізом порошкоподібний діоксид титану, який знаходиться у вигляді агрегатів первинних частинок і має площу поверхні БЕТ, що дорівнює від 20 до 200 м2/г, напівширину (НШ) [нм] розподілу первинних частинок, НШ [нм]=а БЕТf, де а=670 10-9м3/г та -1,3 f -1,0, і частку частинок, які мають діаметр, більший за 45 мкм, що знаходиться в діапазоні від 0,0001 до 0,05 мас.%. Порошок одержують способом, у якому галогенід титану випарюють при температурі нижче 200°С, пару подають у камеру змішування за допомогою газу-носія, який має задану вологість, і незалежно від цього водень, первинне повітря, яке необов’язково може бути збагачене киснем і/або попередньо підігріте, і пару подають у камеру змішування, потім реакційну суміш спалюють у реакційній камері, яка захищена від доступу повітря навколишнього середовища, у реакційну камеру додатково подають вторинне повітря, після чого тверду речовину відокремлюють від газоподібних речовин, і потім тверду речовину обробляють ...

ПОДДЕРЖАНИЕ КАТАЛИТИЧЕСКОЙ АКТИВНОСТИ МОЛЕКУЛЯРНОГО СИТА В УСЛОВИЯХ ПРИСУТСТВИЯ ВОДЯНОГО ПАРА

Настоящее изобретение направлено на способы защиты металл-алюмофосфатных молекулярных сит, конкретно кремний-алюмофосфатных сит (SAPO), от потери каталитической активности вследствие контакта с газом, содержащим воду. Способы по настоящему изобретению обеспечивают методики, которые позволяют активированному ситу контактировать с парами воды, внутри определенного интервала условий в отношении времени, температуры и парциального давления воды, перед тем, как сито становится практически дезактивированным.

CATALYST COMPRISING A PHOSPHORUS MODIFIED ZEOLITE AND HAVING PARTLY AN ALPO STRUCTURE

NANOWIRE CATALYSTSS

METHOD OF PREPARING CATALYST, CATALYST, AND METHOD FOR OXIDATIVE DEHYDROGENATION OF HYDROCARBONS

METHOD FOR MAKING A CATALYST COMPRISING A PHOSPHORUS MODIFIED ZEOLITE AND USE OF SAID ZEOLITE

METHOD FOR MAKING A CATALYST COMPRISING A PHOSPHORUS MODIFIED ZEOLITE AND USE OF SAID ZEOLITE

НОСИТЕЛЬ КАТАЛИЗАТОРА, ОЧИЩЕННЫЙ ОТ АЛЮМИНИЯ, СПОСОБ ПОЛУЧЕНИЯ ЭТОГО НОСИТЕЛЯ КАТАЛИЗАТОРА И СПОСОБ ГИДРАТАЦИИ C2- ИЛИ C3-ОЛЕФИНОВ ВОДОЙ В ПРИСУТСТВИИ КАТАЛИЗАТОРА, ПРЕДСТАВЛЯЮЩЕГО СОБОЙ ЭТОТ НОСИТЕЛЬ, ПРОПИТАННЫЙ КИСЛОТОЙ

Изобретение относится к носителю катализатора, очищенному от алюминия, к способу получения носителя катализатора с пониженным содержанием алюминия на основе слоистых силикатных материалов, встречающихся в природе, например монтмориллонита, а также к способу гидратации С2- или С3-олефинов водой, при котором используют носитель катализатора с пониженным содержанием алюминия. Для реакции гидратации, катализируемой кислотой, носитель пропитывают фосфорной кислотой. Улучшение согласно изобретению по сравнению с обычными способами гидратации состоит в том, что не происходит выщелачивание алюминия из носителя в присутствии фосфорной кислоты. И, таким образом, при реакции не будет происходить блокирование фосфатом алюминия последовательно подсоединенных аппаратов.

СПОСОБ ПРИГОТОВЛЕНИЯ КАТАЛИЗАТОРА НА ОСНОВЕ МОДИФИЦИРОВАННОГО ФОСФОРОМ ЦЕОЛИТА И ПРИМЕНЕНИЕ ТАКОГО ЦЕОЛИТА

Изобретение в первом варианте реализации относится к способу приготовления модифицированного фосфором цеолита, включающему следующие шаги в указанной последовательности: a) взять цеолит, в структуру которого входит хотя бы одно десятичленное кольцо, по усмотрению обработать цеолит паром; b) смешать цеолит, указанный в шаге a), как минимум с одним из связующих компонентов и структуронаправляющих агентов, после чего сформовать смесь; c) по усмотрению выполнить ионообмен; d) по усмотрению обработать паром сформованный катализатор, произвольно - перед шагом c), при этом по меньшей мере одна из указанных обработок паром на шаге d) и на шаге a) обязательна; e) ввести в катализатор по меньшей мере 0,1 мас.% фосфора, применяя сухую импрегнацию или парофазное химическое осаждение; f) ввести металл, по усмотрению - одновременно с шагом e), g) по усмотрению промыть катализатор; h) по усмотрению кальцинировать (прокалить) катализатор; i) обработать катализатор паром - шаг, называемый также приведением ...

КАТАЛИЗАТОРЫ ФИШЕРА-ТРОПША

Способ приготовления кобальтового катализатора на алюмооксидном носителе для использования в реакции синтеза Фишера-Тропша, который включает прокаливание исходного материала γ-алюмооксидного носителя при температуре, позволяющей получать материал модифицированного алюмооксидного носителя; пропитку материала модифицированного алюмооксидного носителя источником кобальта; прокаливание пропитанного материала носителя; активирование катализатора восстановительным газом; обработку активированного катализатора водяным паром и активирование обработанного водяным паром катализатора восстановительным газом.

НАНОПРОВОЛОЧНЫЕ КАТАЛИЗАТОРЫ

Предлагаются нанопроволоки, применимые в качестве гетерогенных катализаторов. Нанопроволочные катализаторы применимы в различных каталитических реакциях, например в окислительной дегидроконденсации метана в этилен. Также раскрыты соответствующие способы их применения и производства.

ОБЪЕМНЫЙ КАТАЛИЗАТОР, ВКЛЮЧАЮЩИЙ ЧАСТИЦЫ ОКСИДОВ МЕТАЛЛОВ, И СПОСОБ ЕГО ПОЛУЧЕНИЯ

Изобретение относится к объемному катализатору, имеющему повышенную активность при гидрообессеривании, в частности при относительно низких мольных отношениях металлов группы VIII к металлам группы VIB. Объемный катализатор включает частицы оксидов металлов, содержащие один или более металлов группы VIB и один или более металлов группы VIII, частицы оксидов металлов получают с помощью способа, включающего стадии взаимодействия соединений, содержащих один или более металлов группы VIB, и соединений, содержащих один или более металлов группы VIII, в гидротермальных условиях при температуре реакции выше температуры кипения протонной жидкости, предпочтительно в автоклаве, при давлении реакции выше атмосферного давления. Изобретение также относится к соответствующему сульфидированному катализатору, к способу получения указанного объемного катализатора и к применению указанного катализатора для гидрообработки, в частности для гидрообессеривания и гидродеазотирования углеводородного сырья.

METHOD OF COMBINED CONVERSION OF HYDROCARBON FRACTIONS AND OXYGENATES IN HIGH OCTANE COMPONENTS ARE FUELS OR AROMATIC HYDROCARBONS AND CATALYST FOR ITS REALIZATION

METHOD OF PREPARING ZEOLITE-CONTAINING CATALYST

Catalytic preparation method of intermediate for antitumor drugs

Method for preparing N-doped nano flower-shaped TiO2 photocatalysis material by taking carbonized lotus leaf as substrate

Regeneration method of poisoned catalyst containing ruthenium or ruthenium compound

Graphene oxide/silver phosphate composite visible light catalyst and preparation method thereof

The invention provides a graphene oxide/silver phosphate composite visible light catalyst and a preparation method of the graphene oxide/silver phosphate composite visible light catalyst, belonging to the technical field of nano-composite material and photocatalysis. The preparation method comprises the following steps of: dissolving graphene oxide in water, and ultrasonically treating to obtain graphene oxide dispersing liquid; adding silver acetate into the graphene oxide dispersing liquid, and evenly stirring, to obtain mixed solution; slowly dropping prepared disodium hydrogen phosphate or sodium dihydrogen phosphate solution into the mixed solution of the graphene oxide and the silver acetate to continuously stir for a while; and repeatedly washing products obtained by reaction with deionized water and absolute ethyl alcohol, and carrying out vacuum drying to obtain the graphene oxide/silver phosphate nano-composite visible light catalyst. The invention has the advantages that the ...

Carbon-based solid acid catalyst and application thereof in lignocellulose depolymerization

Method for activating platinum-containing light alkane dehydrogenation catalyst

A bulk catalyst comprising metal oxidic particles and a process for the manufacture thereof

The invention relates to a bulk catalyst having improved activity in hydrodesulphurisation, in particular in relatively low Group VIII over Group VIB metal molar ratios. The bulk catalyst comprises metal oxidic particles comprising one or more Group VIB metals and one or more-Group VIII metals which metal oxidic particles are obtainable by a process comprising the steps of reacting the compounds comprising one or more Group VIB metals and compounds comprising one or more Group VIII metals in hydrothermal conditions at a reaction temperature above the boiling temperature of the protic liquid, preferably in an autoclave at a reaction pressure above atmospheric pressure and. The invention also relates to the corresponding sulphided catalyst, to a process for the manufacture of the bulk catalyst and to the use of said catalyst for the hydrotreatment, in particular the hydrodesulphurisation and hydrodenitrogenation of hydrocarbon feedstock.

Multilayer cube LaCoO

Method for preparing basic nickel silicate catalyst from solid waste containing silicon

Conditioning of double metal cyanide catalysts

The invention relates to a method for conditioning double metal catalysts which are used in the production of polyether polyols. The conditioning enhances the performance of the catalyst, so that lower concentrations of the DMC catalyst can be used in polyether polyol production.

Catalyst for glycerin dehydration, and process for producing acrolein, process for producing acrylic acid, and process for producing hydrophilic resin each using the catalyst

A catalyst for glycerin dehydration of the present invention comprises boron phosphate or a rare-earth metal phosphate, wherein a molar ratio P/B of phosphorus (P) to boron (B) or a molar ratio P/R of phosphorus (P) to a rare-earth metal (R) is more than 1.0 and 2.0 or less. An another catalyst for glycerin dehydration of the present invention comprises a combination of boron phosphate and a metal element or a combination of a rare-earth metal phosphate and a metal element other than a rare-earth metal, wherein a molar ratio M/(P+B) of a metal element (M) to phosphorus (P) and boron (B) or a molar ratio M/(P+R) of a metal element (M) to phosphorus (P) and a rare-earth metal (R) is more than 0.00005 and 0.5 or less.

Cop2 loaded red phosphorus, preparation and use of the same

Disclosed are a photocatalyst of CoP 2 loaded red phosphorus, a preparation method thereof, and a method for photocatalytic hydrogen production from water under visible light irradiation over the photocatalyst of CoP 2 loaded red phosphorus.

METHOD OF SYNTHESIS OF NANO-SIZED BETA ZEOLITES CONTAINING MESOPORES AND USES THEREOF

A method for hydrocracking a hydrocarbon feedstock, the method comprising: contacting the hydrocarbon feedstock with a catalyst containing a nano-sized mesoporous zeolite composition under reaction conditions to produce a product stream containing at least 20 weight percent of hydrocarbons with 1-4 carbon atoms, wherein the nano-sized mesoporous zeolite composition is produced by a method that includes: mixing silica, a source of aluminum, and tetraethylammonium hydroxide to form an aluminosilicate fluid gel; drying the aluminosilicate fluid gel to form a dried gel mixture; subjecting the dried gel mixture to hydrothermal treatment to produce a zeolite precursor; adding cetyltrimethylammonium bromide (CTAB) to the zeolite precursor to form a templated mixture; subjecting the templated mixture to hydrothermal treatment to prepare a CTAB-templated zeolite; washing the CTAB-templated zeolite with distilled water; separating the CTAB-templated zeolite by centrifugation; and drying and calcining the CTAB-templated zeolites to produce a nano-sized mesoporous zeolite composition. 1. A method for hydrocracking a hydrocarbon feedstock , the method comprising: mixing silica, a source of aluminum, and tetraethylammonium hydroxide to form an aluminosilicate fluid gel;', 'drying the aluminosilicate fluid gel to form a dried gel mixture;', 'subjecting the dried gel mixture to hydrothermal treatment to produce a zeolite precursor;', 'adding cetyltrimethylammonium bromide (CTAB) to the zeolite precursor to form a templated mixture;', 'subjecting the templated mixture to hydrothermal treatment to prepare a CTAB-templated zeolite;', 'washing the CTAB-templated zeolite with distilled water;', 'separating the CTAB-templated zeolite by centrifugation; and', 'drying and calcining the CTAB-templated zeolites to produce a nano-sized mesoporous zeolite composition., 'contacting the hydrocarbon feedstock with a catalyst containing a nano-sized mesoporous zeolite composition under reaction ...

MWW TYPE ZEOLITE, METHOD FOR PRODUCING SAME, AND CRACKING CATALYST

Provided are the following: an MWW type zeolite which has many Brønsted acid sites when in the form of a proton type and which is highly suitable as a cracking catalyst for cumene; a method for producing same; and an application of same. The present invention provides an MWW type zeolite in which the ratio (B/A) of the peak intensity (B) attributable to tetracoordinate aluminum relative to the peak intensity (A) attributable to hexacoordinate aluminum is 2 or more in Al MAS NMR, when measured as an ammonium type. The present invention also provides a method for producing an MWW type zeolite, the method having a step for carrying out a hydrothermal synthesis reaction in the presence of: a seed crystal of an MWW type zeolite containing no organic structure-directing agent; and a reaction mixture containing a silica source, an alumina source, an alkali source, an organic structure-directing agent, and water. The reaction mixture satisfies the following molar ratio: X/SiO<0.15 (here, X denotes the number of moles of the organic structure-directing agent). 1. An MWW-type zeolite wherein a ratio (B/A) of a peak intensity (B) attributable to tetracoordinate aluminum to a peak intensity (A) attributable to hexacoordinate aluminum is 2 or more in Al MAS NMR as measured in the form of an ammonium type.2. The MWW-type zeolite according to claim 1 , wherein an amount of Brønsted acid site with a adsorption heat of ammonia of 106 kJ/mol or more is 0.5 mmol/g or more.3. The MWW-type zeolite according to claim 1 , wherein a micropore volume is 0.07 cm/g or more and 0.2530 cm/g or less.4. The MWW-type zeolite according to claim 1 , wherein SiO/AlOmolar ratio is 17 or more and 37 or less.5. The MWW-type zeolite according to claim 1 , wherein when the MWW-type zeolite is subjected to X-ray diffraction measurement claim 1 , a peak is observed in at least one range below:2θ=6.4° to 7.4°, 13.5° to 14.5°, 24.1° to 25.1°, 24.7 to 25.7°, 27.1 to 28.1°, 28.0° to 29.0°, 28.6° to 29.6°, and ...

PROCESS FOR PREPARING A BORON CONTAINING ZEOLITIC MATERIAL HAVING MWW FRAMEWORK STRUCTURE

A process for preparing an aluminum-free boron containing zeolitic material comprising the framework structure MWW (BMWW), comprising (a) hydrothermally synthesizing the BMWW from a synthesis mixture containing water, a silicon source, a boron source, and an MWW template compound obtaining the BMWW in its mother liquor, the mother liquor having a pH above 9; (b) adjusting the pH of the mother liquor, obtained in (a) and containing the BMWW, to a value in the range of from 6 to 9; (c) separating the BMWW from the pH-adjusted mother liquor obtained in (b) by filtration in a filtration device. 1: A process for preparing an aluminum-free boron comprising zeolitic material comprising a framework structure MWW (BMWW) , the process comprising(a) hydrothermally synthesizing a BMWW precursor from a synthesis mixture comprising water, a silicon source, a boron source, and an MWW template compound obtaining the BMWW precursor in a mother liquor, the mother liquor having a pH above 9;(b) adjusting the pH of the mother liquor, obtained in (a) and comprising the BMWW precursor, to a value in a range of from 6 to 9 to obtain a pH-adjusted mother liquor;(c) separating the BMWW precursor from the pH-adjusted mother liquor obtained in (b) by filtration in a filtration device.2: The process of claim 1 , wherein in (a) claim 1 , at least 95 weight-% of the synthesis mixture consist of water claim 1 , the silicon source claim 1 , the boron source claim 1 , and the template compound.3: The process of claim 1 , wherein in (a) claim 1 , the silicon source is selected from the group consisting of fumed silica claim 1 , colloidal silica claim 1 , and a mixture thereof claim 1 , the boron source is selected from the group consisting of boric acid claim 1 , a borate claim 1 , boron oxide claim 1 , and a mixture of two or more thereof claim 1 , and the MWW template compound is selected from the group consisting of piperidine claim 1 , hexamethylene imine claim 1 , N claim 1 ,N claim 1 ,N claim ...

ALKALI METAL ION MODIFIED TITANIUM SILICALITE ZEOLITE FOR GAS PHASE EPOXIDATION OF PROPYLENE AND HYDROGEN PEROXIDE AND PREPARATION METHOD THEREOF

An alkali metal ion modified titanium silicalite zeolite for gas phase epoxidation of propylene and hydrogen peroxide and a preparation method thereof. The method includes, at first step: preparing an alkali metal hydroxide modification solution; at second step: conducting controlled hydrothermal treatment on a TS-1 zeolite matrix by using an alkali metal hydroxide solution; and at third step: conducting post-treatment on the hydrothermally modified TS-1 zeolite, including solid-liquid separation, washing, drying and calcining. In the washing process, the modified TS-1 zeolite wet material is washed with a low concentration alkali metal hydroxide solution; alkali metal ions are reserved on the silicon hydroxyl of the modified titanium silicalite zeolite; and an infrared characteristic absorption band of a framework titanium active center modified by the alkali metal ions is in a range above 960 cmand below 980 cm. 1. An alkali metal ion modified titanium silicalite zeolite as catalyst for gas phase epoxidation of propylene and hydrogen peroxide , wherein in the alkali metal ion modified titanium silicalite zeolite , alkali metal ions are reserved on the silicon hydroxyl of the modified TS-1 zeolite; an infrared characteristic absorption band of framework titanium active site modified by the alkali metal ions is in a range above 960 cmand below 980 cm; TS-1 zeolite matrix of the alkali metal ion modified titanium silicalite zeolite meets the following requirements: the crystal size is ≥0.3 micron; a silicon-titanium molar ratio is ≤200; an index value of the framework titanium content is ≥0.40; and relative crystallinity is ≥85%.2. The alkali metal ion modified titanium silicalite zeolite for the gas phase epoxidation of propylene and hydrogen peroxide according to claim 1 , wherein the crystal size of the TS-1 zeolite matrix is ≥0.5 micron; the silicon-titanium molar ratio is ≤100; the index value of the framework titanium content is ≥0.45; and the relative ...

A CATALYST COMPOSITION AND ITS APPLICATIONS THEREOF

The present disclosure discloses a catalyst composition comprising: (a) at least one steamed biochar; and (b) at least one tri-metallic catalyst, comprising metals selected from the group consisting of nickel, copper, zinc, and combinations thereof, wherein nickel loading is in the range of 20-60 wt %, the copper loading is in the range of 0.5-5.0 wt %, and the zinc loading is in the range of 0.5-5.0 wt with respect to the at least one steamed biochar. The instant disclosure further relates to a process of preparation of the catalyst composition and a process for production of hydrogen gas and carbon nanotubes. 1) A catalyst composition comprising:(a) at least one steamed biochar; and 'wherein the nickel loading is in the range of 20-60 wt %, the copper loading is in the range of 0.5-5.0 wt %, and the zinc loading is in the range of 0.5-5.0 wt % with respect to the at least one steamed biochar.', '(b) at least one tri-metallic catalyst comprising metals selected from the group consisting of nickel, copper, zinc, and combinations thereof,'}2) The composition as claimed in claim 1 , wherein the nickel loading is in the range of 27-31 wt % claim 1 , the copper loading is in the range of 2.0-2.7 wt % claim 1 , and zinc loading is in the range of 2.0-2.7 wt % with respect to the at least one steamed biochar.3) The catalyst composition as claimed in claim 1 , wherein the at least one tri-metallic catalyst is disposed on claim 1 , within claim 1 , or combination of on or within claim 1 , the at least one steamed biochar.4) The catalyst composition as claimed in claim 1 , wherein the at least one steamed biochar has a surface area in the range of 700-950 m/g and a pore volume in the range of 0.60-0.70 cc/g.5) The catalyst composition as claimed in claim 1 , wherein the at least one steamed biochar is obtained from raw biochar saw dust claim 1 , raw biochar rice straw claim 1 , raw biochar rice husk claim 1 , raw biochar bagasse claim 1 , other agricultural wastes claim 1 , ...

CATALYST STRUCTURE AND METHOD FOR PRODUCING SAME, AND METHOD FOR PRODUCING HYDROCARBON BY USE OF CATALYST STRUCTURE

A catalyst structure that allows prevention of aggregation of fine particles of a functional substance, suppresses decrease of catalyst activity, and thus enables extension of the lifetime of the catalyst structure. A catalyst structure has a carrier that is formed from a zeolite-type compound and has a porous structure. The functional substance includes a first element that is at least one metallic element selected from the group consisting of cobalt (Co), nickel (Ni), iron (Fe), and ruthenium (Ru), and at least one second element selected from the group consisting of metallic elements in group , group , group , group , and group on the periodic table. The carrier has paths connected to each other. The functional substance is present in at least the paths of the carrier. 1. A catalyst structure comprising:a support that has a porous structure and comprises a zeolite-type compound; andat least one functional material present in the support,at least one functional material comprising:at least one first metal element selected from the group consisting of cobalt (Co), nickel (Ni), iron (Fe), and ruthenium (Ru); andat least one second metal element selected from the group consisting of metal elements belonging to Groups 1, 2, 4, 7, and 12 of periodic table, whereinthe support has channels communicating with one another, andthe functional material is present at least in the channels of the support.2. The catalyst structure according to claim 1 , wherein the second element is at least one metal element selected from the group consisting of potassium (K) claim 1 , magnesium (Mg) claim 1 , titanium (Ti) claim 1 , zirconium (Zr) claim 1 , manganese (Mn) claim 1 , and zinc (Zn).3. The catalyst structure according to claim 1 , wherein a mass ratio of a content of the second element to a content of the first element is from 0.01 to 2.00.4. The catalyst structure according to claim 1 , wherein a total content of the first element is 0.5% by mass or more with respect to the mass ...

METHOD FOR APPLYING PHOTOCATALYTIC COATINGS WITHOUT USING BINDERS, AND USE OF A COATING

The invention relates to a method for applying titanium dioxide-based photocatalytic coatings to a carrier material without using binders. The invention also relates to the use of a coating. According to the invention, a titanium dioxide suspension together with a carrier liquid is sprayed onto a hot carrier in the form of a fine aerosol so that the carrier liquid flash evaporates and titanium dioxide particles of the titanium dioxide suspension are flash sintered onto the carrier material, water being used as the carrier liquid and the carrier material having a temperature of 150 to 250° C. during spraying. According to the invention, a porous and yet stable layer for a catalyst for an efficient and rapid degradation of pollutants is produced. 1. A method for binder-free application of titanium dioxide-based photocatalytic coatings to a support material , where a titanium dioxide suspension with a carrier liquid is sprayed in the form of a fine aerosol onto a hot support , so that the carrier liquid undergoes flash evaporation and titanium dioxide particles of the titanium dioxide suspension undergo flash sintering onto the support material , the carrier liquid used being water , during the sprayed application, the support material has a temperature of 150 to 250° C., thus forming a porous and yet stable layer for a catalyst for efficient and rapid pollutant degradation,', 'the heat is generated in the support material itself, and', 'the support material is traversed by an electrical current., 'characterized in that'}2. The method as claimed in claim 1 , characterized in that during the sprayed application claim 1 , the support material has a temperature which lies above the boiling temperature of the carrier liquid.3. The method as claimed in claim 1 , characterized in that the titanium dioxide suspension has a fraction of 5 to 20 mass % of titanium dioxide particles.4. The method as claimed in claim 1 , characterized in that the method is multiply repeated.5. ( ...

CONTROLLED PRESSURE HYDROTHERMAL TREATMENT OF ODH CATALYST

The preparation of an oxidative dehydrogenation catalyst comprising Mo, V, Nb and Te using a hydrothermal step the activity and reproducibility of the catalyst is improved by conduction the hydrothermal step at higher pressures while permitting gaseous products to leave the reactor. In some instances a condenser may be upstream of the pressure relief valve. 1. A process for synthesis of a catalyst for oxidative dehydrogenation of paraffins via a hydrothermal treatment comprising:i) preparing an aqueous slurry comprising Mo, V, Nb and Te salts in a molar ratio of metal elements 1:0.3 to 3; 0.05 to 0.25; and 0.08 to 0.2 at a temperature from 25° C. to 80° C.;ii) heating slurry in a reactor to a temperature from 80° to 220° C. at a pressure equal or above the saturated water vapor pressure at the corresponding reaction temperature, for a period of time not less than 1 hour with agitation and simultaneous removal of gaseous byproduct species produced during the reaction.iii) letting the reactor cool and depressurizing the reactor and recovering the catalyst as a solid.2. The process according to claim 1 , wherein the temperature of the reactor is from 150° C.-185° C.3. The process according to claim 2 , wherein the pressure in the reactor is from 10 psi to 190 psi (960 kPa to 1300 kPa).4. The process according to claim 1 , wherein there is a condenser upstream of a pressure control device.5. The process according to 4 claim 1 , wherein the condenser is operated at a temperature above 0° C. and below reaction temperature.6. The process according to claim 1 , wherein the gaseous species are removed by being vented from the reactor through the pressure control device.71. The process according claim 1 , wherein the gaseous species are removed from the reactor using one or more methods selected from gas absorption claim 1 , gas adsorption claim 1 , membrane separation claim 1 , and chemicals transformation.8. The process according to wherein the time of hydrothermal ...

Methane oxidation catalyst, process to prepare the same and method of using the same

The present invention provides a method of treating an exhaust gas comprising methane and NO. The exhaust gas is contacted with a catalyst in the presence of oxygen to oxidize at least part of the methane in the gas stream to carbon dioxide and water and at least part of the NO into NO2 obtaining a treated gas stream. The catalyst comprises one or more noble metals supported on non-modified zirconia, wherein the zirconia comprises tetragonal zirconia and monoclinic zirconia, and wherein the weight ratio of tetragonal zirconia to monoclinic zirconia is in the range of from 1:1 to 31:1.

Fenton-like Catalytic Material with Dual Reaction Centers and Preparation Method Thereof

A method for preparing a Fenton-like catalytic material with dual reaction centers includes the following steps: (1) placing a nitrogen-containing compound in a muffle furnace for calcination, then dissolving the product in deionized water to form a suspension solution; (2) dissolving aluminum nitrate nonahydrate, copper nitrate trihydrate and glucose in deionized water to form a solution; (3) adding the suspension solution in a dropwise manner to the solution, then performing a closed hydrothermal reaction, washing with water, centrifuging and drying to obtain a solid; and (4) placing the prepared solid in a muffle furnace for calcination to obtain the Fenton-like catalytic material. The catalytic material presents a complete ball-flower shaped mesoporous structure, has a large specific surface area, and can expose more catalytic active sites, so that H2O2 is reduced at the electron-rich center as much as possible to generate hydroxyl radicals during the reaction.

CATALYSTS FOR THE OXIDATIVE DEHYDROGENATION OF ALKANES

This document relates to oxidative dehydrogenation catalysts that include molybdenum, vanadium, and oxygen. 1. An oxidative dehydrogenation catalyst comprising molybdenum , vanadium , and oxygen , wherein:the molar ratio of molybdenum to vanadium in the catalyst is from 1:0.15 to 1:0.75, as determined by inductively coupled plasma mass spectrometry (ICP-MS),oxygen is present in the catalyst at least in an amount to satisfy the valency of any present metal oxides, andthe amorphous phase of the catalyst is greater than 55 wt. %, as determined by X-ray diffraction (XRD).2. The oxidative dehydrogenation catalyst of claim 1 , wherein the amorphous phase is from 55 wt. % to 80 wt. % claim 1 , as determined by XRD.3. The oxidative dehydrogenation catalyst of claim 1 , wherein the amorphous phase is from 55 wt. % to 75 wt. % claim 1 , as determined by XRD.4. The oxidative dehydrogenation catalyst of claim 1 , wherein the catalyst has a 35% conversion temperature from about 300° C. to about 400° C.5. The oxidative dehydrogenation catalyst of claim 1 , wherein the catalyst has a selectivity to ethylene from 65% to 99%.6. The oxidative dehydrogenation catalyst of claim 1 , wherein the catalyst is prepared by a method comprising:providing an aqueous mixture comprising molybdenum and vanadium,hydrothermally reacting the mixture to form a precalcined catalyst, andcalcining the precalcined catalyst to form the catalyst.7. The oxidative dehydrogenation catalyst of claim 6 , wherein providing the aqueous mixture comprising molybdenum and vanadium comprises combining an aqueous mixture comprising molybdenum and an aqueous mixture comprising vanadium.8. The oxidative dehydrogenation catalyst of claim 7 , wherein the aqueous mixture comprising molybdenum is prepared from at least (NH)MoO.4HO and a first water.9. The oxidative dehydrogenation catalyst of claim 7 , wherein the aqueous mixture comprising vanadium is prepared from at least VOSO.XHO and a second water.10. An oxidative ...

PROCESS FOR PREPARATION OF ZEOLITIC MATERIAL

The present invention relates to a process for process for the preparation of a zeolitic material which process comprises (i) providing a boron-containing zeolitic material and (ii) deboronating the boron-containing zeolitic material by treating the boron-containing zeolitic material with a liquid solvent system thereby obtaining a deboronated zeolitic material, which liquid solvent system does not contain an inorganic or organic acid, or a salt thereof. 1. A process for the preparation of a zeolitic material , comprising:(i) providing a boron-containing zeolitic material of a structure MWW or BEA;(ii) deboronating the boron-containing zeolitic material with a liquid solvent system at a temperature in the range of from 50 to 125° C. thereby obtaining a deboronated zeolitic material of the structure MWW or BEA;wherein the liquid solvent system is water, andwherein said liquid solvent system does not contain an inorganic or organic acid or a salt thereof, the acid being selected from the group consisting of hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, formic acid, acetic acid, propionic acid, oxalic acid, and tartaric acid.24-. (canceled)5. The process of claim 1 , wherein in (i) claim 1 , the boron-containing zeolitic material is provided by a process comprising(a) hydrothermally synthesizing the boron-containing zeolitic material from a synthesis mixture containing at least one silicon source, at least one boron source, and at least one template compound, to obtain the boron-containing zeolitic material in its mother liquor;(b) separating the boron-containing zeolitic material from its mother liquor;(c) drying the boron-containing zeolitic material separated according to (b);(d) calcining the boron-containing zeolitic material obtained from (b) or (c).6. (canceled)7. The process of claim 1 , wherein the boron-containing zeolitic material provided in (i) is an aluminum-free zeolitic material.8. The process of claim 1 , wherein the boron-containing ...

Process for preparing a hierarchical zeolite catalyst for aromatization of C5-C9 alkane

A process for preparing a hierarchical zeolite catalyst for aromatization of C5-C9 alkane that provides high conversion percentage of precursor to yields and high aromatics selectivity, wherein said process comprises the following steps: 1. A process for preparing a hierarchical zeolite catalyst for aromatization of C5-C9 alkane , wherein said process comprises the following steps:(a) preparing a solution containing alumina compound, silica compound, and soft template;(b) subjecting the mixture obtained from step (a) to hydrothermal process at determined time and temperature to form said mixture into the hierarchical zeolite;(c) contacting the hierarchical zeolite obtained from step (b) with ammonium salt solution; and(d) contacting the hierarchical zeolite obtained from step (c) with gallium salt solution;characterized in that the soft template in step (a) is a quaternary phosphonium salt in which the mole ratio of the silica compound to the alumina compound in step (a) is in a range of 20 to 120 and the gallium salt in step (d) has gallium to zeolite ratio in a range of 0.5 to 5% by weight.2. The process for preparing according to claim 1 , wherein the quaternary phosphonium salt is tetraalkylphosphonium selected from tetrabutylphosphonium hydroxide and tributyl hexadecyl phosphonium bromide.3. The process for preparing according to claim 2 , wherein the quaternary phosphonium salt is tetrabutylphosphonium hydroxide.4. The process for preparing according to claim 1 , wherein the mole ratio of the silica compound to the alumina compound in step (a) is in the range of 20 to 60.5. The process for preparing according to claim 1 , wherein the gallium salt in step (d) has gallium to zeolite ratio in the range of 0.5 to 1% by weight.6. The process for preparing according to claim 1 , wherein the gallium salt is selected from gallium nitrate claim 1 , gallium chloride claim 1 , gallium bromide claim 1 , gallium hydroxide claim 1 , and gallium acetate.7. The process for ...

CRYSTALLINE METALLOPHOSPHATES, THEIR METHOD OF PREPARATION, AND USE

A new family of crystalline microporous metallophosphates designated AlPO-85 has been synthesized. These metallophosphates are represented by the empirical formula 5. The method of wherein E is aluminum.6. The method of wherein a source of aluminum is selected from the group consisting of aluminum alkoxides claim 3 , precipitated aluminas claim 3 , aluminum metal claim 3 , aluminum hydroxide claim 3 , aluminum salts and alumina sols.7. The method of wherein a source of phosphorus is selected from the group consisting of orthophosphoric acid claim 3 , phosphorus pentoxide claim 3 , and ammonium dihydrogen phosphate.8. The method of wherein sources of silica are selected from the group consisting of tetraethylorthosilicate claim 3 , colloidal silica claim 3 , and precipitated silica.9. The method of wherein the sources of other E elements are selected from the group consisting of organoammonium borates claim 3 , boric acid claim 3 , precipitated gallium oxyhydroxide claim 3 , gallium sulfate claim 3 , ferric sulfate claim 3 , and ferric chloride.10. The method of wherein sources of the M metals are selected from the group consisting of halide salts claim 3 , nitrate salts claim 3 , acetate salts claim 3 , and sulfate salts of the respective alkaline earth and transition metals.11. The method of wherein R is an organoammonium cation prepared from a reaction of an aqueous mixture of a cyclic secondary amine and an organic dihalide.12. The method of wherein said cyclic secondary amines are selected from the group consisting of piperidine claim 11 , homopiperidine claim 11 , pyrrolidine claim 11 , and morpholine.13. The method of wherein the organic dihalides are selected from the group consisting of 1 claim 11 ,4-dibromobutane claim 11 , 1 claim 11 ,5-dibromopentane claim 11 , and 1 claim 11 ,6-dibromohexane.14. The method of wherein said reaction mixture is reacted at a temperature from about 125° C. to about 175° C.16. The process of wherein said separation of ...

METHOD FOR OBTAINING MESOPOROUS SILICA PARTICLES WITH SURFACE FUNCTIONALIZATION

It is provided a method for obtaining mesoporous silica particles with surface functionalisation comprising the steps of a) providing solutions of at least three precursors; wherein the pH of the mixture is adjusted to a range between 2 and 8 in a buffered system; b) Mixing the precursor solutions thereby allowing a reaction to take place at a temperature between 20 and 60° C., whereby surface functionalized mesoporous silica particles as solid reaction product are formed; c) Separating the surface functionalized mesoporous silica particles from the reaction mixture by centrifugation or filtration; d) Removing any pore structure directing agent present in the pores of the formed surface functionalized mesoporous silica particles by ultrasonication; e) followed by separation by centrifugation or filtration, washing and drying of the surface functionalized mesoporous silica particles. 1. Method for obtaining mesoporous silica particles with surface functionalisation comprising the steps ofa) providing solutions of at least three precursors, wherein the at least three precursor agents are selected from a group containing:at least one alkali silicate solution,at least one solution containing at least one pore structure directing agent (SDA), andat least one agent for surface functionalisation;wherein the pH of the mixture is adjusted to a range between 2 and 8 in a buffered system;b) Mixing the precursor solutions thereby allowing a reaction to take place at a temperature between 20 and 60° C., preferably between 20° C. and 25° C., whereby surface functionalized mesoporous silica particles as solid reaction product are formed;c) Separating the surface functionalized mesoporous silica particles from the reaction mixture by centrifugation or filtration and optionally washing the surface functionalized mesoporous silica;d) Removing any pore structuring directing agent present in the pores of the formed surface functionalized mesoporous silica particles by ultrasonication ...

PLATINUM-CONTAINING CATALYSTS FOR COMBUSTION ENGINES

Emissions treatment systems of combustion engines are provided, which comprise a platinum-containing catalyst that is degreened during production, which is before exposure to operating conditions of a vehicle having a diesel engine. The platinum-containing catalyst, in the form of a platinum component on a high surface area refractory metal oxide support, exhibits a vibration frequency of about 2085 to about 2105 cm−1 as measured by CO-DRIFTS. Such catalytic material is essentially-free of platinum oxide species found at greater than about 2110 cm−1 as measured by CO-DRIFTS. Such catalysts can provide excellent and consistent conversion of nitrogen oxide (NO) to nitrogen dioxide (NO2). 1. A diesel oxidation catalyst composite comprising: a diesel oxidation catalytic material on a carrier , the catalytic material comprising a platinum component on a high surface area refractory metal oxide support ,{'sup': '−1', 'wherein the catalytic material exhibits a peak vibration frequency in the range of about 2085 to about 2105 cmas measured by CO-DRIFTS prior to exposure to operating conditions of a vehicle having a diesel engine.'}2. The diesel oxidation catalyst composite of claim 1 , wherein the catalytic material is essentially-free of platinum oxide species found at >about 2110 cmas measured by CO-DRIFTS.3. The diesel oxidation catalyst composite of claim 1 , wherein the catalyst composite is fully degreened during production of the catalyst material.4. The diesel oxidation catalyst composite of claim 1 , wherein upon exposure to continuous operation of a vehicle having a diesel engine in a range of about 200° C. to about 350° C. claim 1 , the catalytic material continues to exhibit a peak vibration frequency of about 2085 to about 2105 cmas measured by CO-DRIFTS.5. The diesel oxidation catalyst composite of claim 1 , wherein the platinum component is in particle form and has an average particle size in the range of about 0.5 nm to about 6 nm as measured by a CO- ...

METHOD FOR DEGRADING AN ORGANIC MATERIAL AND METHOD FOR STERILIZING

A method for manufacturing a molybdenum disulfide powder includes conducting a precursor solution preparation step and a hydrothermal synthesis step. The precursor solution preparation step includes providing sodium molybdenum oxide dihydrate and thiourea, and conducting a mixing step. In the mixing step, an acid solution is mixed with the sodium molybdenum oxide dihydrate and the thiourea by titrating so as to form a precursor solution. In the hydrothermal synthesis step, the precursor solution is put into a hydrothermal container for reacting at a temperature ranging from 100° C. to 350° C. for 8 hours to 40 hours, thus the molybdenum disulfide powder is formed. 1. A method for degrading an organic material , comprising:providing a molybdenum disulfide powder, wherein the molybdenum disulfide powder is stacked from a plurality of layered structures, and at least one of the layered structures is an odd-layer structure;conducting a contacting step, wherein the molybdenum disulfide powder is contacted with a medium, and the medium comprises at least one organic material and water; andconducting a degrading step, wherein a mechanical perturbation is generated in the medium to polarize the molybdenum disulfide powder, and a pair of electron and hole are generated for degrading the organic material.2. The method for degrading the organic material of claim 1 , wherein the medium is an aqueous solution.3. The method for degrading the organic material of claim 2 , wherein the organic material is rhodamine or methylene blue.4. The method for degrading the organic material of claim 2 , wherein the mechanical perturbation is generated by an ultrasonic wave.5. The method for degrading the organic material of claim 1 , wherein the medium is an air.6. The method for degrading the organic material of claim 5 , wherein the organic material is an organic gas.7. A method for sterilizing claim 5 , comprising:providing a molybdenum disulfide powder, wherein the molybdenum disulfide ...

CERIUM OXIDE PARTICLES AND METHOD FOR PRODUCTION THEREOF

The present invention relates to cerium oxide particles that have excellent heat resistance under hydrothermal conditions at high temperature. The present invention also relates to a method for preparing such cerium oxide particles and to a catalytic composition comprising said cerium oxide. 1. Cerium oxide particles exhibiting:{'sub': 2', '2', '2, 'sup': '2', 'a specific surface area (BET) after ageing at 800° C. for 16 hours, under a gaseous atmosphere containing 10% by volume of O, 10% by volume of HO and the balance of N, of at least 75 m/g; or'}{'sub': 2', '2', '2, 'sup': '2', 'a specific surface area (BET) after ageing at 700° C. for 16 hours, under a gaseous atmosphere containing 10% by volume of O, 10% by volume of HO and the balance of N, of at least 97 m/g.'}2. Cerium oxide particles according to claim 1 , exhibiting a specific surface area (BET) after ageing at 800° C. for 16 hours claim 1 , under a gaseous atmosphere containing 10% by volume of O claim 1 , 10% by volume of HO and the balance of N claim 1 , between 75 and 80 m/g.3. Cerium oxide particles according to claim 1 , exhibiting a specific surface area (BET) after ageing at 700° C. for 16 hours claim 1 , under a gaseous atmosphere containing 10% by volume of O claim 1 , 10% by volume of HO and the balance of N.4. Cerium oxide particles according to claim 1 , exhibiting a specific surface area (BET) after ageing at 700° C. for 16 hours claim 1 , under a gaseous atmosphere containing 10% by volume of O claim 1 , 10% by volume of HO and the balance of N claim 1 , between 97 and 102 m/g.5. Cerium oxide particles according to one of the preceding claims claim 1 , exhibiting a specific surface area (BET) after ageing at 900° C. for 16 hours claim 1 , under a gaseous atmosphere containing 10% by volume of O claim 1 , 10% by volume of HO and the balance of N claim 1 , of at least 39 m/g.6. Cerium oxide particles according to claim 1 , exhibiting a specific surface area (BET) after ageing at 900° C. for ...

WATER STABLE COPPER PADDLEWHEEL METAL ORGANIC FRAMEWORK (MOF) COMPOSITIONS AND PROCESSES USING THE MOFS

This invention relates to a Cu-BTC MOF which is water stable. The Cu-BTC MOF has been modified by substituting some of the BTC ligand (1,3,5, benzene tricarboxylic acid) with 5-aminoisophthalic acid (AIA). The resultant MOF retains at least 40% of its as synthesized surface area after exposure to liquid water at 60° C. for 6 hours. This is an unexpected result versus the MOF containing only the BTC ligand. This MOF can be used to abate contaminants such as ammonia in gas streams and especially air streams. 1. A metal organic framework (MOF) composition comprising:a coordination product of a copper metal ion and a mixture of organic ligands selected from 1,3,5-benzenetricarboxylic acid (BTC) and 5-aminoisophthalic acid (AIA) the MOF characterized in that it retains at least 40% of its as synthesized surface area after exposure to liquid water at 60° C. for 6 hours.2. The composition of further characterized in that the MOF has an as synthesized Brunauer-Emmett-Teller (BET) surface area of at least 1500 m/g.3. The composition of further characterized in that the MOF has an as synthesized Brunauer-Emmett-Teller (BET) surface area of at least 1700 m/g.4. The composition of further characterized in that the MOF has a gravimetric uptake capacity for ammonia of at least 0.25 g of ammonia per gram of MOF measured at 650 torr and 25° C.5. The composition of where the molar ratio of BTC:AIA varies from about 99:1 to about 1:99.6. The composition of where the molar ratio of BTC:AIA is 1:1.7. The composition of where the molar ratio of BTC:AIA is 1:38. The composition of where the molar ratio of BTC:AIA is: 3:1.9. The composition of claim lwherein it retains at least 50% of its surface area after exposure to liquid water at 60° C. for 6 hours.10. The MOF of further characterized in that the MOF is formed into a shaped body selected from pellets claim 1 , spheres claim 1 , disks claim 1 , monolithic body claim 1 , irregularly shaped particles claim 1 , extrudates claim 1 , and ...

ACID/METAL BIFUNCTIONAL CATALYST PRODUCED BY EXTRUSION

A method of producing bifunctional catalysts by extrusion may include mixing an acid catalyst, a metal catalyst, optionally a binder, and a fluid to produce a dough; extruding the dough to form an extrudate; producing a powder from the extrudate; and calcining the powder to produce an acid/metal bifunctional catalyst. Such acid/metal bifunctional catalysts may be useful in, among other things, converting syngas to dimethyl ether in a single reactor. 1. A method comprising:mixing an acid catalyst, a metal catalyst, a binder, and a fluid to produce a dough;extruding the dough to form an extrudate;producing a powder from the extrudate; andcalcining the powder to produce an acid/metal bifunctional catalyst.2. The method claim 1 , wherein producing the powder from the extrudate comprises:drying the extrudate; andgrinding the extrudate before or after drying, wherein the powder comprises 5 wt % or less of the fluid.3. The method of further comprising:drying the powder.4. The method of further comprising:heating the dough while extruding to a temperature within 20° C. of a boiling point of the fluid.5. The method of claim 1 , wherein the acid catalyst is selected from the group consisting of a zeolite claim 1 , an ion exchanged zeolite claim 1 , a molecular sieve claim 1 , a metal oxide claim 1 , and any combination thereof6. The method of claim 1 , wherein the metal catalyst is a M1/M2/A1 catalyst claim 1 , wherein M1 is selected from the group consisting of Cu claim 1 , Cr claim 1 , Ag claim 1 , Au claim 1 , Ru claim 1 , Rh claim 1 , Pd claim 1 , Re claim 1 , Os claim 1 , Ir claim 1 , Pt claim 1 , and any combination thereof claim 1 , wherein M2 is selected from the group consisting of Ti claim 1 , V claim 1 , Cr claim 1 , Mn claim 1 , Fe claim 1 , Co claim 1 , Ni claim 1 , Zn claim 1 , a rare earth metal claim 1 , a La series metal claim 1 , a Y series metal claim 1 , and any combination thereof claim 1 , and wherein M1 and M2 are different.7. The method of claim 1 , ...

ACID/METAL BIFUNCTIONAL CATALYST SYSTEMS PRODUCED WITH CARBON COATINGS

A method of producing bifunctional catalyst systems that include a carbon-coated metal catalyst may comprise: coating a metal catalyst particle with a carbon-containing small molecule to produce a coated metal catalyst particle; carbonizing the carbon-containing small molecule on the coated metal catalyst particle to produce a carbon-coated metal catalyst particle; and mixing the carbon-coated metal catalyst particle with an acid catalyst particle to produce an acid/metal bifunctional catalyst system. Further, a method of producing bifunctional catalyst systems that include a carbon-coated acid catalyst may be similarly performed by coating a metal catalyst particle with a carbon-containing small molecule to produce a coated metal catalyst particle; carbonizing the carbon-containing small molecule on the coated metal catalyst particle to produce a carbon-coated metal catalyst particle; and mixing the carbon-coated metal catalyst particle with an acid catalyst particle to produce an acid/metal bifunctional catalyst system. 1. A method comprising:coating a metal catalyst particle with a carbon-containing small molecule to produce a coated metal catalyst particle;carbonizing the carbon-containing small molecule on the coated metal catalyst particle to produce a carbon-coated metal catalyst particle; andmixing the carbon-coated metal catalyst particle with an acid catalyst particle to produce an acid/metal bifunctional catalyst system.2. The method claim 1 , wherein the acid catalyst particle is a carbon-coated acid catalyst particle.3. The method of claim 1 , wherein carbonizing comprises:exposing the coated metal catalyst particle to an elevated temperature of 200° C. to 400° C. in an inert atmosphere for 10 minutes to 24 hours.4. The method claim 1 , wherein coating comprises:exposing the metal catalyst particle to an aqueous suspension of the carbon-containing small molecule.5. The method of claim 1 , wherein an amount of the carbon-containing small molecule used ...

Process for Obtaining a Catalyst Composite

A process for obtaining a catalyst composite comprising the following steps: 135-. (canceled)36. A process for the catalytic cracking of an olefin-rich feedstock which is selective towards light olefins in the effluent , the process comprising: at least 10 wt % of a molecular sieve having pores of 10-or more-membered rings;', 'at least one metal silicate different from said molecular sieve comprising at least one alkaline earth metal, such that the catalyst composite comprises at least 0.1 wt % of silicate to produce an effluent with an olefin content of lower molecular weight than that of the hydrocarbon feedstock., 'contacting a hydrocarbon feedstock containing one or more olefins with a catalyst composite comprising37. The process according to claim 36 , wherein the molecular sieve is a P-modified zeolite claim 36 , and wherein the metal silicate comprises one or more of Ga claim 36 , Al claim 36 , Ce claim 36 , In claim 36 , Cs claim 36 , Sc claim 36 , Sn claim 36 , Li claim 36 , Zn claim 36 , Co claim 36 , Mo claim 36 , Mn claim 36 , Ni claim 36 , Fe claim 36 , Cu claim 36 , Cr claim 36 , Ti claim 36 , and V.38. The process according to claim 36 , wherein the molecular sieve is a zeolite claim 36 , wherein the metal silicate is xonotlite (CaSiO(OH)).39. The process according to claim 36 , wherein the catalyst composite comprises metal phosphate.40. The process according to claim 36 , wherein the catalyst composite comprises matrix material.41. The process according to claim 36 , wherein the catalyst composite comprises binder.42. The process of comprising: at least 10 wt % of a molecular sieve having pores of 10-or more-membered rings;', 'at least one metal silicate, different from said molecular sieve, comprising at least one alkaline earth metal, such that the XTO catalyst composite comprises at least 0.1 wt % of silicate,, 'contacting an oxygen-containing, halogenide-containing or sulphur-containing organic feedstock in an XTO reactor with an XTO catalyst ...

MOLECULAR SIEVE SSZ-123, ITS SYNTHESIS AND USE

An aluminum-rich molecular sieve material of MFS framework type, designated SSZ-123, is provided. SSZ-123 can be synthesized using 1-ethyl-1-[5-(triethylammonio)pentyl]piperidinium cations as a structure directing agent. SSZ-123 may be used in organic compound conversion and/or sorptive processes.

Preparation method of caprolactam

The present disclosure discloses a method for preparing caprolactam including: (1) contacting cyclohexanone oxime with a catalyst to carry out reaction in the presence of ethanol and under the condition of gas phase Beckmann rearrangement reaction of cyclohexanone oxime; (2) separating the reaction product obtained in step (1) to produce an ethanol solution of crude caprolactam, and then separating the ethanol solution of crude caprolactam to obtain ethanol and crude caprolactam; (3) removing impurities with boiling points lower than that of caprolactam in the crude caprolactam to obtain a light component removal product; (4) mixing the light component removal product with a crystallization solvent to carry out crystallization and solid-liquid separation to obtain a crystalline crystal; (5) subjecting the crystalline crystal to a hydrogenation reaction; wherein the crystallization solvent contains 0.1-2 wt % of ethanol.

PROCESS FOR PREPARING A ZEOLITIC MATERIAL COMPRISING TI AND HAVING FRAMEWORK TYPE CHA

A process for preparing a zeolitic material comprising Ti, having framework type CHA and having a framework structure which comprises Si and O, said process comprising (i) preparing a pre-synthesis mixture comprising water, a CHA framework structure directing agent, and a zeolitic material comprising Ti, having framework type MFI and having a framework structure which comprises Si and O; (ii) removing water from the pre-synthesis mixture obtained from (i) by heating the pre-synthesis mixture to a temperature of less than 100° C. at a pressure of less than 1 bar (abs); (iii) hydrothermally crystallizing the zeolitic material comprising Ti, having framework type CHA and having a framework structure which comprises Si and O. 1. A process for preparing a zeolitic material comprising Ti , having framework type CHA and having a framework structure which comprises Si and O , said process comprising:{'sub': 2', '2', '2', '2', '2, '(i) preparing a pre-synthesis mixture comprising water, a CHA framework structure directing agent, and a zeolitic material comprising Ti, having framework type MFI and having a framework structure which comprises Si and O, wherein a molar ratio of the CHA framework structure directing agent relative to Si, comprised in the zeolitic material having framework type MFI and calculated as SiO, said molar ratio being defined as SDA:SiO, is at least 0.4:1, and wherein a molar ratio of water relative to Si, comprised in the zeolitic material having framework type MFI and calculated as SiO, said molar ratio being defined as HO:SiO, is at least 30:1;'}{'sub': 2', '2', '2, '(ii) removing water from the pre-synthesis mixture by heating the pre-synthesis mixture to a temperature of less than 100° C. at a pressure of less than 1 bar(abs) and keeping the temperature of the pre-synthesis mixture in this range and the pressure of the pre-synthesis mixture in this range, obtaining a synthesis mixture comprising water, the CHA framework structure directing agent, ...

TRANSITION METAL-CARRYING ZEOLITE AND PRODUCTION METHOD THEREFOR, AND NITROGEN OXIDE PURIFICATION CATALYST AND METHOD FOR USING SAME

This transition metal-loaded zeolite is configured such that an absorption intensity ratio in a specific region of the transition metal-loaded zeolite observed by ultraviolet-visible-near infrared spectroscopy (UV-Vis-NIR) and an intensity ratio of a maximum peak in a different temperature range of the transition metal-loaded zeolite measured by ammonia temperature-programmed desorption, respectively fall within specific ranges. 1. A transition metal-loaded zeolite , comprisingzeolite having a structure designated as AEI or AFX according to a code system defined by International Zeolite Association (IZA), and comprising at least a silicon atom and an aluminum atom in a framework structure thereof, anda transition metal M loaded thereon,wherein the transition metal-loaded zeolite satisfies (1) and (2): {'br': None, 'sup': −1', '−1, 'Intensity (32,500 cm)/Intensity (12,500 cm)\u2003\u2003(I) and'}, '(1) a ratio of absorption intensity based on ultraviolet-visible-near infrared spectroscopy (UV-Vis-NIR), which is obtained according to expression (I), is less than 0.4;'}{'sub': 3', '3', '200-400', '3', '450-600, '(2) a peak intensity obtained according to ammonia temperature-programmed desorption (NH-TPD) exists in at least each of a range of 200° C. to 400° C. and a range of 450° C. to 600° C. and a ratio of a maximum peak intensity in the range of 200° C. to 400° C. to a maximum peak intensity in the range of 450° C. to 600° C. (NH-TPD/NH-TPD) is 1.0 or more and 2.0 or less.'}2. The transition metal-loaded zeolite according to claim 1 , further satisfying (3):(3) a molar ratio M/Al is 0.1 or more and 0.35 or less.3. The transition metal-loaded zeolite according to claim 1 , wherein the ratio of absorption intensity based on ultraviolet-visible-near infrared spectroscopy (UV-Vis-NIR) is less than 0.3.4. The transition metal-loaded zeolite according to claim 1 , wherein the ratio of absorption intensity based on ultraviolet-visible-near infrared spectroscopy (UV-Vis-NIR ...

COPPER-CONTAINING KFI-TYPE ZEOLITE AND USE IN SCR CATALYSIS

The present invention relates to a copper-containing KFI-type zeolite, wherein the zeolite contains 1 to 4.5 wt.-% copper. The invention is also directed towards a method for producing the copper-containing zeolite according to the invention as well as towards the use of the zeolite in SCR catalysis. Further subjects of the invention are a washcoat which contains the zeolite according to the invention, an SCR catalyst which contains the zeolite according to the invention as well as an exhaust-gas cleaning system which comprises the SCR catalyst. 1. A copper-containing KFI-type zeolite , wherein the zeolite contains 1 to 4.5 wt.-% copper relative to the total weight of the zeolite and wherein the zeolite is largely free of phases of the structure types CHA , ERI and LTL and has a phase purity >50%.2. The copper-containing zeolite of claim 1 , wherein the zeolite comprises primary crystallites with cuboid structure.3. The copper-containing zeolite of claim 1 , wherein the zeolite comprises primary crystallites with cubic structure.4. The copper-containing zeolite of claim 1 , wherein the zeolite comprises primary crystallites with a size in the range of from 0.2 to 10 μm.5. The copper-containing zeolite of claim 1 , wherein the zeolite contains iron.6. The copper-containing zeolite of claim 1 , wherein the proportion of copper and iron together is 1.01 to 10 wt.-% relative to the total weight of the zeolite.7. Copper-containing zeolite according to claim 1 , wherein the zeolite has phase proportions of a zeolite of structure type MER.8. (canceled)9. A method for producing a copper-containing zeolite of claim 1 , comprising:providing a KFI-type zeolite which can have phase proportions of an MER-type zeolite,thermally treating or hydrothermally treating the zeolite at a temperature ≧500° C.10. The method of claim 9 , wherein a replacement of copper and optionally iron takes place before the thermal/hydrothermal treatment or after the thermal/hydrothermal treatment.11. ...

Catalyst for single step conversion of glycerol to acrylic acid and process for the preparation thereof

The present invention provides a process and a solid catalyst for oxydehydration of glycerol to acrylic acid with H 2 O 2 under mild experimental condition at atmospheric pressure. The process provides a single step liquid phase selective oxidation glycerol to acrylic acid over nanocrystalline Cu supported α-MnO 2 catalyst. The process provides glycerol conversion of 20-78% and selectivity of acrylic acid up to 86%.

SMALL CRYSTAL LTL FRAMEWORK TYPE ZEOLITES

Small crystal LTL framework type zeolites, characterized as polycrystalline aggregates, each of the aggregates comprising a plurality of spherical or cube-like crystallites and wherein each crystallite has an average crystallite size of from 10 to 50 nm, are disclosed. Such zeolites can be prepared by hydrothermal conversion of FAU framework type zeolites at low HO/SiOmole ratios. 2. The method of claim 1 , wherein each of the aggregates has a first claim 1 , a second claim 1 , and a third dimension claim 1 , and each of the first claim 1 , the second claim 1 , and the third dimensions is from 100 to 300 nm.3. The method of claim 1 , wherein the aggregates are essentially spherical in shape.4. The method of claim 1 , wherein at least 80% of the aggregates have an aspect ratio of from 0.7 to 1.5. The method of claim 1 , wherein the FAU framework type zeolite is zeolite Y.7. The method of claim 1 , wherein the hydrothermal conditions include a temperature of from 135° C. to 200° C.8. The method of claim 1 , wherein the LTL framework type zeolite is prepared in the absence of LTL framework type seed crystals.9. An LTL framework type zeolite claim 1 , characterized as polycrystalline aggregates claim 1 , each of the aggregates comprising a plurality of spherical or cube-like crystallites and wherein each crystallite has an average crystallite size of from 10 to 50 nm.10. The zeolite of claim 9 , wherein each crystallite has an average crystallite size of from 15 to 35 nm.11. The zeolite of claim 9 , wherein each of the aggregates has a first claim 9 , a second claim 9 , and a third dimension claim 9 , and each of the first claim 9 , the second claim 9 , and the third dimensions is from 100 to 300 nm.12. The zeolite of claim 9 , wherein each of the aggregates has a first claim 9 , a second claim 9 , and a third dimension claim 9 , and each of the first claim 9 , the second claim 9 , and the third dimensions is from 150 to 250 nm.13. The zeolite of claim 9 , wherein the ...

AROMATIZATION CATALYST, PREPARATION METHOD, REGENERATION METHOD THEREOF, AND AROMATIZATION METHOD

The present disclosure provides an aromatization catalyst, a preparation method, a regeneration method and an aromatization method thereof. The preparation method comprises steps of: mixing a zeolite molecular sieve with a binder to obtain a catalyst precursor; the catalyst precursor is successively subjected to an ion exchange modification and a first modification treatment, and then subjected to a hydrothermal treatment, and further subjected to active metal loading and a second modification treatment, to obtain the aromatization catalyst. The aromatization catalyst has good carbon deposition resistance and high aromatization activity, and enables an aromatization reaction to be completed under mild conditions, and has high aromatic selectivity, and the liquid yield is above 98.5%. 1. A preparation method for an aromatization catalyst , consisting of steps of:mixing a nano zeolite molecular sieve with a binder at a dry basis weight ratio of (1:9)˜(9:1) to obtain a catalyst precursor;the catalyst precursor is successively subjected to an ion exchange modification and a first modification treatment, then subjected to a hydrothermal treatment, and further subjected to active metal loading and a second modification treatment, to obtain the aromatization catalyst; whereinan exchange element used for the ion exchange modification is at least one alkali metal selected from Group IA of the Periodic Table of the Elements, with a loading amount of 0.1˜2 wt % based on a weight of the exchange element with respect to a weight of the catalyst precursor;a first modifying element used in the first modification treatment is at least one element selected from Group IA, Group VA, and lanthanide metals of the Periodic Table of the Elements, with a loading amount of 0.05˜10 wt % based on a weight of the first modifying element with respect to the weight of the catalyst precursor;the active metal is at least one element selected from Group VIIB, Group VIII, Group IB and Group IIB of ...

UZM-53, AN MTT ZEOLITE

A new crystalline aluminosilicate zeolite comprising a MTT framework has been synthesized that has been designated UZM-53. This zeolite is represented by the empirical formula: 2. The zeolite of wherein two peaks of very strong intensity are present.3. The zeolite of wherein said zeolite has a y in said empirical formula that is less than 25.4. The zeolite of wherein said zeolite has a y in said empirical formula that is less than 22.6. The zeolite of wherein in said empirical formula for said zeolite claim 5 , y′ is from about 12 to 25.7. The zeolite of wherein said zeolite has a NHLewis acid value of less than 0.05.8. The zeolite of wherein said zeolite has a NHLewis acid value of less than 0.04.9. The zeolite of wherein said zeolite has a NHLewis acid value of less than 0.03.10. The zeolite of wherein said zeolite has a Collidine Brønsted value of less than 0.12.11. The zeolite of wherein said zeolite has a Collidine Brønsted value of less than 0.113. The process of where M is a combination of sodium and potassium and the ratio of sodium to potassium is in the range from about 0.1 to about 2.14. The process of where the source of E is selected from the group consisting of alkali borates claim 12 , boric acid claim 12 , precipitated gallium oxyhydroxide claim 12 , gallium sulfate claim 12 , ferric sulfate claim 12 , ferric chloride and mixtures thereof.15. The process of where the aluminum source is selected from the group consisting of aluminum alkoxides claim 12 , precipitated aluminas claim 12 , aluminum metal claim 12 , aluminum hydroxide claim 12 , sodium aluminate claim 12 , potassium aluminate claim 12 , aluminum salts and aluminum sols.16. The process of where the silicon source is selected from the group consisting of tetraethylorthosilicate claim 12 , fumed silica claim 12 , colloidal silica claim 12 , alkali silicates and precipitated silica.17. The process of further comprising adding UZM-53 seeds to the reaction mixture.18. The process of wherein the ...

HIGH-PERFORMANCE ZEOLITE FOR REDUCING NITROGEN OXIDE EMISSIONS, METHOD OF PREPARING SAME AND CATALYST USING SAME

Disclosed is a method of preparing a high-performance zeolite catalyst for reducing nitrogen oxide emissions, and more particularly a technique for preparing a zeolite catalyst, suitable for use in effectively removing nitrogen oxide (NOx), among exhaust gases emitted from vehicle internal combustion engines through selective catalytic reduction (SCR), thereby exhibiting high efficiency, high chemical stability and high thermal durability upon SCR using the prepared catalyst. 1. A copper-impregnated LTA zeolite catalyst for selective catalytic reduction of nitrogen oxide having high hydrothermal stability and base durability , the catalyst comprisinga high-silica-content LTA zeolite in which copper is ion-exchanged,wherein a silicon/aluminum (Si/Al) molar ratio is 8 to 30 and a particle size is 0.5 to 5.0 μm.2. The catalyst of claim 1 , wherein the particle size is 0.5 to 2.0 μm claim 1 , a specific surface area is 700 m2/g or more claim 1 , the Si/Al molar ratio is 8 to 16 claim 1 , a Cu/Al molar ratio is 0.45 to 0.5 claim 1 , and a residual fluorine (F) content in a skeleton of the catalyst is 0.02% or less.3. The catalyst of or claim 1 , wherein the copper-impregnated LTA zeolite has a crystallinity of 50% or more after a hydrothermal treatment at 900° C. and a crystallinity of 30% or more after a base treatment.4. The catalyst of claim 3 , wherein a nitrogen oxide conversion efficiency is 70% or more upon reaction with a reaction gas containing nitrogen oxide at 150° C. to 600° C. after the hydrothermal treatment at 900° C.5. The catalyst of claim 1 , which is applied to a selective catalytic reduction (SCR) or an SCR-catalyzed diesel particulate filter (SDPF) for an internal combustion engine exhaust system.6. A method of preparing a copper-impregnated LTA zeolite catalyst claim 1 , the method comprisingproducing an LTA zeolite andimpregnating copper in the LTA zeolite, wherein the producing of the LTA zeolite is performed using a fluorine-substituted structure ...

PROCESS FOR PREPARING AN ELECTRIDE COMPOUND

A process for preparing an electride compound, comprising (i) providing a precursor compound comprising an oxidic compound of the garnet group; (ii) heating the precursor provided in (i) under plasma forming conditions in a gas atmosphere to a temperature of the precursor above the Hüttig temperature of the precursor, obtaining the electride compound. 115.-. (canceled)16. A process for preparing an electride compound , comprising(i) providing a precursor compound of the electride compound, wherein the precursor compound comprises an oxidic compound of the garnet group;(ii) heating the precursor compound provided in (i) under plasma forming conditions in a gas atmosphere to a temperature of the precursor compound above the Hüttig temperature of the precursor compound, obtaining the electride compound.17. The process of claim 16 , wherein according to (ii) claim 16 , heating the precursor compound under plasma forming conditions comprises heating the precursor compound in an electric arc.18. The process of claim 16 , wherein the oxidic compound of the garnet group according to (i) comprises aluminum and/or calcium.19. The process of claim 16 , wherein at least 90 weight-% of the precursor compound consist of an oxidic compound of the garnet group.20. The process of claim 16 , wherein providing the precursor compound according to (i) comprises(i.1) preparing a mixture comprising a source of calcium, a source of aluminum, and water;(i.2) optionally subjecting the mixture prepared in (i.1) to a hydrothermal treatment;(i.3) calcining the mixture prepared in (i.1), optionally the mixture obtained from (i.2), obtaining the precursor compound.21. The process of claim 20 , wherein the source of calcium is one or more of a calcium oxide claim 20 , a calcium hydroxide claim 20 , a hydrated calcium oxide claim 20 , and a calcium carbonate claim 20 , and the source of aluminum is one or more of an aluminum hydroxide including one or more of gibbsite claim 20 , hydrargillite claim ...

METHOD FOR ISOMERISING DEHYDRATION OF A NON-LINEAR PRIMARY MONOALCOHOL ON A QUADRILOBED IRON ZEOLITE CATALYST

A method for isomeris ng dehydration in the presence of a specific catalyst, to produce at least one alkene, carried out on a feedstock containing a non-linear primary monoalcohol, where the catalyst includes a zeolite having a series of 8MR channels and a binder having certain pore volume, which catalyst is multilobe-shaped and has characteristics including certain average mesopore volume Vm, and mesopores having a certain diameter, an average certain macropore volume VM, the macropores having a certain diameter, and certain average micropore volume Vμ, the micropores having a certain diameter, and the catalyst has a certain exposed geometric area. 1. A process for isomerizing dehydration of a feedstock comprising , alone or in a mixture , a primary monoalcohol of formula R—CH—OH , in which R is a nonlinear alkyl radical of general formula CHwhere n is an integer of between 3 and 20 , said process comprising a step of isomerizing dehydration operated in the gas phase at a weighted average temperature of between 250 and 460° C. , at a pressure of between 0.2 MPa and 1 MPa , at a weight hourly space velocity (WWH) of between 1 and 25 h , in the presence of a catalyst comprising at least one zeolite and at least one binder , in which the amount by weight Tz of zeolite is 55-90 wt % relative to the total weight of said catalyst and in which said zeolite has at least one series of channels with an aperture of 8 oxygen atoms (8MR) , said binder having a pore volume of between 0.5 and 0.9 ml/g , the catalyst being multilobate and havingan average mesopore volume Vm centered at plus or minus 20% around the value defined by the formula Vm=−0.004Tz+0.505, the mesopores having a diameter of 3.6 nm to 50 nm,an average macropore volume VM centered at plus or minus 20% around the value defined by the formula VM=0.0101Tz 0.5375, the macropores having a diameter of more than 50 nm and less than 7000 nm,an average micropore volume Vμ centered at plus or minus 20% around the value ...

MODIFIED CATALYST WITH STRUCTURE TYPE MTW, A METHOD FOR ITS PREPARATION AND ITS USE IN A PROCESS FOR THE ISOMERIZATION OF AN AROMATIC C8 CUT

The invention concerns a catalyst comprising at least one zeolite with structure type MTW, a matrix, at least one metal from group VIII of the periodic classification of the elements, said catalyst having a mesopore volume increased by at least 10% compared with its initial mesopore volume, which is generally in the range 0.55 to 0.75 mL/g, at the end of a treatment with steam at a partial pressure in the range 0.01 to 0.07 MPa and at a temperature in the range 300° C. to 400° C. for at least 0.5 hour. The invention concerns the process for the preparation of said catalyst as well as an isomerization process employing said catalyst. 117-. (canceled)18. A process for the preparation of a catalyst comprising at least one zeolite with structure type MTW , a matrix , and at least one metal from group VIII of the periodic classification of the elements , comprising at least the following steps:i) providing at least one zeolite with structure type MTW,ii) preparing a support by shaping said zeolite with a matrix,iii) depositing at least one metal from group VIII of the periodic classification of the elements onto said support or onto said zeolite, wherein the depositing can be before or after the preparing of the support in step ii),iv) bringing the catalyst obtained in step ii) or step iii), depending on the order in which they are carried out, into contact with steam at a partial pressure in the range 0.01 to 0.07 MPa, at a temperature in the range 300° C. to 400° C., for at least 0.5 hour, in a manner such that the mesopore volume of the catalyst is increased by at least 10% compared with the mesopore volume of the catalyst before the contact with steam.19. The process according to claim 18 , wherein step ii) is followed by drying carried out at a temperature in the range 100° C. to 150° C. for a period in the range 5 to 20 hours in an oven claim 18 , then by calcining carried out at a temperature in the range 250° C. to 600° C. for a period in the range 1 to 8 hours. ...

ZnWO4 PHOTOCATALYTIC MATERIAL WITH OXYGEN VACANCY AND PREPARATION METHOD THEREOF

The invention belongs to the field of novel photocatalytic materials, and particularly relates to a ZnWO4 photocatalytic material containing oxygen vacancy. According to the material, absorption exists in a near infrared region of an ultraviolet-visible light diffuse reflection spectrum, wherein the wavelength range of the near infrared region is 780-2500 nm. The invention further relates to a preparation method of the ZnWO4 photocatalytic material containing oxygen vacancy. Na2WO4 and soluble zinc salt are used as raw materials, ZnWO4 crystals are formed through a hydrothermal crystallization reaction and then roasted in the presence of hydrogen so as to achieve partial reduction of ZnWO4, and then the ZnWO4 photocatalytic material containing oxygen vacancy is obtained. 1. A ZnWOphotocatalytic material containing oxygen vacancy , characterized in that absorption exists in a near infrared region of an ultraviolet-visible light diffuse reflection spectrum of the material , wherein a wavelength range of the near infrared region is 780-2500 nm.2. The ZnWOphotocatalytic material containing oxygen vacancy of claim 1 , characterized in that ZnWOis roasted in the presence of hydrogen so as to achieve partial reduction of ZnWO claim 1 , and then the ZnWOphotocatalytic material containing oxygen vacancy is obtained.3. The ZnWOphotocatalytic material containing oxygen vacancy of claim 2 , characterized in that a roasting temperature is 350-600 DEG C. claim 2 , and a roasting time is 1-4 h.4. The ZnWOphotocatalytic material containing oxygen vacancy of claim 2 , characterized in that a temperature increasing rate during roasting is 1-5 DEG C./min.5. A preparation method of the ZnWOphotocatalytic material containing oxygen vacancy claim 2 , characterized in that NaWOand soluble zinc salt are used as raw materials claim 2 , ZnWOcrystals are formed through a hydrothermal crystallization reaction and then roasted in the presence of hydrogen so as to achieve partial reduction of ...

COMPOSITIONS COMPRISING PLATINUM NANOPARTICLE CLUSTERS WITH IMPROVED THERMOSTABILITY

A composition comprising platinum (Pt) nanoparticles and an inorganic oxide, wherein the Pt nanoparticles have no more than 100 Pt atoms, wherein the Pt nanoparticles have a mean particle size of 1 nm to 10 nm with a standard deviation (SD) no more than 1 nm. 1. A composition comprising platinum (Pt) nanoparticles and an inorganic oxide , wherein the Pt nanoparticles have no more than 100 Pt atoms , wherein the Pt nanoparticles have a mean particle size of 1 nm to 10 nm with a standard deviation (SD) no more than 1 nm.2. The composition of claim 1 , wherein the Pt nanoparticles have a mean particle size of 1 nm to 5 nm.3. The composition of claim 1 , wherein the Pt nanoparticles have a mean particle size of no more than 15 nm after hydrothermal redox aging at 600° C. for 4 hours claim 1 , wherein the mean particle size is measured by TEM.4. The composition of claim 1 , wherein the Pt nanoparticles have a mean particle size of no more than 20 nm after hydrothermal redox aging at 700° C. for 4 hours claim 1 , wherein the mean particle size is measured by TEM.5. The composition of claim 1 , wherein the Pt nanoparticles have a mean particle size of no more than 25 nm after hydrothermal redox aging at 800° C. for 4 hours claim 1 , wherein the mean particle size is measured by TEM.6. The composition of claim 1 , wherein the Pt nanoparticles have 2 to 100 Pt atoms.7. The composition of claim 6 , wherein the Pt nanoparticles have 30 to 100 Pt atoms.8. The composition of claim 1 , wherein the Pt nanoparticles have a mean particle size of no more than 50 nm after aging at 1000° C. for 4 hours claim 1 , wherein the mean particle size is measured by TEM.9. The composition of claim 1 , wherein the Pt nanoparticles have a mean particle size of no more than 30 nm after hydrothermal redox aging at 800° C. for 4 hours claim 1 , wherein the mean particle size is measured by CO-pulse method.10. The composition of claim 1 , wherein the Pt nanoparticles have a mean particle size of no ...

Mesoporous Catalyst Compounds and Uses Thereof

The present disclosure provides mesoporous catalyst compounds and compositions having one or more group 13 atoms. The present disclosure further relates to processes for converting hydrocarbon feedstocks to small olefins. In one aspect, a catalyst compound includes a zeolite having a structural type selected from MFI, MSE, MTW, Theta-One (TON), Ferrierite (FER), AFI, AFS, ATO, BEA, BEC, BOG, BPH, CAN, CON, EMT, EON, EZT, FAU, GME, GON, IFR, ISV, ITN, IWR, IWW, LTL, MAZ, MEI, MOR, MOZ, OFF, OKO, OSI, SAF, SAO, SEW, SFE, SFO, SSF, SSY, and USI, or a combination thereof, the zeolite having a silicon to aluminum molar ratio (Si/Al ratio) of from about 5 to about 40. In one aspect, a catalyst composition includes the catalyst compound and one or more group 13 metal. 1. A catalyst compound comprising:a zeolite having a structural type selected from MFI, MSE, MTW, TON, FER, AFI, AFS, ATO, BEA, BEC, BOG, BPH, CAN, CON, EMT, EON, EZT, FAU, GME, GON, IFR, ISV, ITN, IWR, IWW, LTL, MAZ, MEI, MOR, MOZ, OFF, OKO, OSI, SAF, SAO, SEW, SFE, SFO, SSF, SSY, and USI, or a combination thereof, the zeolite having a silicon to aluminum molar ratio (Si/Al ratio) of from about 5 to about 40.2. The catalyst compound of claim 1 , wherein the zeolite is a mesoporous MCM-68.3. The catalyst compound of claim 1 , wherein the zeolite has a ring size of at least an 8-membered ring.4. The catalyst compound of claim 1 , wherein the zeolite has a plurality of 12-membered rings.5. The catalyst compound of claim 1 , wherein the zeolite has at least one of the following properties: a total surface area of from 400 m2/g to 600 m2/g claim 1 , a total mesopore volume of 0.1 mL/g or greater claim 1 , or a total pore volume of from about 0.2 mL/g to about 0.6 mL/g.6. The catalyst compound of claim 1 , wherein the zeolite has a hexane sorption capacity at 75 Torr claim 1 , and 90° C. claim 1 , of about 5 wt % to about 15 wt % claim 1 , based on the total weight of the catalyst.7. A catalyst composition ...

HYDROCARBON CONVERSION USING UZM-53

A new crystalline aluminosilicate zeolite comprising a MTT framework has been synthesized that has been designated UZM-53. This zeolite is represented by the empirical formula: 2. The process of wherein the hydrocarbon conversion process is selected from the group consisting of hydrocracking claim 1 , hydrotreating claim 1 , hydrodenitrogenation claim 1 , hydrodesulfurization claim 1 , naphthene ring opening claim 1 , paraffin isomerization claim 1 , olefin isomerization claim 1 , conversion of an aromatic molecule to another aromatic molecule claim 1 , polyalkylbenzene isomerization claim 1 , disproportionation of alkylbenzenes claim 1 , aromatic alkylation claim 1 , paraffin alkylation claim 1 , paraffin cracking claim 1 , naphthene cracking claim 1 , reforming claim 1 , hydrogenation claim 1 , dehydrogenation claim 1 , transalkylation claim 1 , dealkylation claim 1 , hydration claim 1 , and dehydration.3. The process of wherein said microporous crystalline zeolite has a y in said empirical formula that is less than 25.4. The process of wherein said microporous crystalline zeolite has a y in said empirical formula that is less than 22.6. The process of wherein in the empirical formula for said microporous crystalline zeolite claim 5 , y′ is from about 12 to 25.7. The process of wherein said microporous crystalline zeolite has a NHLewis acid value of less than 0.05.8. The process of wherein said microporous crystalline zeolite has a NHLewis acid value of less than 0.04.9. The process of wherein said microporous crystalline zeolite has a NHLewis acid value of less than 0.03.10. The process of wherein said microporous crystalline zeolite has a Collidine Brønsted value of less than 0.12.11. The process of wherein said microporous crystalline zeolite has a Collidine Brønsted value of less than 0.1.12. The process of wherein said microporous crystalline zeolite has a micropore volume as a percentage of total pore volume of less than 70% as determined by BET analysis ...

ORGANIC-FREE SYNTHESIS OF SMALL PORE ZEOLITE CATALYSTS

The present invention is directed to methods of enhancing the catalytic activities of 8-MR zeolites, the methods comprising treating a precursor 8-MR zeolite that has been prepared without the use of an organic structure directing agent and having an Si/Al ratio of less than 5, with high temperature steam for a period of time sufficient to extract at least a portion of the aluminum from the precursor zeolite framework to form a steam-treated zeolite having an Si/tetrahedral Al ratio of greater than 5, wherein the steam has a temperature in a range of from about 350° C. to about 850° C. The compositions produced by these methods and their use in catalytic reactions are also provided.

THREE DIMENSIONAL METAL SULFIDES CATALYTIC STRUCTURES, METHODS OF MAKING AND USES THEREOF

A bulk three-dimensional (3-D) catalyst and methods of making and use are described herein. The bulk three-dimensional (3-D) catalyst is formed from a catalytically active metal or metal alloy and has a sulfurized or oxidized outer surface. 1. A bulk three-dimensional (3-D) catalyst comprising a catalytically active metal or metal alloy having a 3-D structure comprising the catalytically active metal or metal alloy having a sulfurized or oxidized outer surface.2. The bulk three-dimensional (3-D) catalyst of claim 1 , wherein the catalytic metal or metal alloy comprises an alkaline earth metal claim 1 , a transition metal claim 1 , a post-transition metal claim 1 , any combination thereof claim 1 , or any alloy thereof.3. The bulk three-dimensional (3-D) catalyst of claim 2 , wherein the catalytically active metal is nickel (Ni) claim 2 , iron (Fe) claim 2 , chromium (Cr) claim 2 , aluminum (Al) claim 2 , copper (Cu) claim 2 , manganese (Mn) claim 2 , zinc (Zn) or alloys thereof.4. The bulk three-dimensional (3-D) catalyst of claim 1 , wherein the catalytically active metal is sinter resistant.5. The bulk three-dimensional (3-D) catalyst of claim 1 , wherein the catalyst does not include a ceramic support claim 1 , a metal support claim 1 , a metal coating claim 1 , a binder claim 1 , or combinations thereof.6. The bulk three-dimensional (3-D) catalyst of claim 1 , wherein the 3-D structure is a foam structure claim 1 , a honeycomb structure claim 1 , or mesh structure.7. The bulk three-dimensional (3-D) catalyst of claim 6 , wherein the 3-D structure is a foam having a pore size from 100 μm to 10000 μm claim 6 , a surface area of 1 to 100 m/g claim 6 , or both.8. The bulk three-dimensional (3-D) catalyst of claim 1 , wherein the outer surface comprises a catalytically active metal sulfide or oxide layer or a catalytically active metal alloy sulfide or oxide layer claim 1 , and the morphology of the sulfide layer comprises a flaky uneven structure claim 1 , a well ...

CATIONIC POLYMERS AND POROUS MATERIALS

According to one or more embodiments, cationic polymers may be produced which include one or more monomers containing cations. Such cationic polymers may be utilized as structure directing agents to form mesoporous zeolites. The mesoporous zeolites may include micropores as well as mesopores, and may have a surface area of greater than 350 m/g and a pore volume of greater than 0.3 cm/g. Also described are core/shell zeolites, where at least the shell portion includes a mesoporous zeolite material. 2. The cationic polymer of claim 1 , where A and B are nitrogen.3. The cationic polymer of claim 1 , further comprising one or more anions selected from Cl claim 1 , Br claim 1 , F claim 1 , I claim 1 , OH claim 1 , ½ SO claim 1 , ⅓ PO claim 1 , ½ S claim 1 , AlO.4. The cationic polymer of claim 1 , where R5 comprises a carbon chain length of from 3 to 30 carbon atoms.5. The cationic polymer of claim 1 , where R5 comprises a carbon chain length of from 5 to 10 carbon atoms.6. The cationic polymer of claim 1 , where R6 claim 1 , R7 claim 1 , R8 claim 1 , and R9 are hydrogen.7. The cationic polymer of claim 1 , where R10 is an alkyl group.8. The cationic polymer of claim 1 , where R10 is a methyl group.9. The cationic polymer of claim 1 , where R11 claim 1 , R12 and R13 are alkyl groups.10. The cationic polymer of claim 1 , where R11 claim 1 , R12 and R13 are methyl groups.11. The cationic polymer of claim 1 , where R11 claim 1 , R12 and R13 are ethyl groups.12. The cationic polymer of claim 1 , where R11 claim 1 , R12 and R13 are propyl groups.13. The cationic polymer of claim 1 , where the cationic polymer is poly(N claim 1 ,N-diallyl-N-alkyl-N claim 1 ,N claim 1 ,N-trialkylalkane-1 claim 1 ,6-diamonium halide).14. The cationic polymer of claim 1 , where the cationic polymer is poly(N claim 1 ,N-diallyl-N-methyl-N claim 1 ,N claim 1 ,N-trimethylhexane-1 claim 1 ,6-diamonium bromide).15. The cationic polymer of claim 1 , where the cationic polymer is poly(N claim 1 ,N- ...

FUNCTIONAL STRUCTURAL BODY AND METHOD FOR MAKING FUNCTIONAL STRUCTURAL BODY

Provide is a functional structural body that can suppress aggregation of metal oxide nanoparticles and prevent functional loss of metal oxide nanoparticles, and thus exhibit a stable function over a long period of time. A functional structural body () includes: a skeletal body () of a porous structure composed of a zeolite-type compound; and at least one type of metal oxide nanoparticles () containing a perovskite-type oxide present in the skeletal body (), the skeletal body () having channels () that connect with each other, and the metal oxide nanoparticles () being present at least in the channels () of the skeletal body (). 1. A functional structural body , comprising:a skeletal body of a porous structure composed of a zeolite-type compound; andat least one type of metal oxide nanoparticles containing a perovskite-type oxide present in the skeletal body, whereinthe skeletal body has channels connecting with each other, andthe metal oxide nanoparticles are present at least in the channels of the skeletal body.2. The functional structural body according to claim 1 , whereinthe channels have any one of a one-dimensional pore, a two-dimensional pore, and a three-dimensional pore defined by a framework of the zeolite-type compound and an enlarged pore portion with a diameter different from that of any of the one-dimensional pore, the two-dimensional pore, and the three-dimensional pore, andthe metal oxide nanoparticles are present at least in the enlarged pore portion.3. The functional structural body according to claim 2 , wherein the enlarged pore portion makes a plurality of pores claim 2 , which constitute any one of the one-dimensional pore claim 2 , the two-dimensional pore claim 2 , and the three-dimensional pore claim 2 , connect with one another.4. The functional structural body according to claim 2 , wherein an average particle size of the metal oxide nanoparticles is greater than an average inner diameter of the channels and is less than or equal to the ...

CATALYST SYSTEMS AND METHODS OF USE

According to embodiments, methods for the production of boron-silicalite-1 are disclosed. In embodiments, the method may include combining a mineralizer agent, a templating agent, water, and boric acid in a first microwave unit; heating the first microwave unit to form a boron-zeolite; calcining the boron-zeolite to form an alkali-zeolite; combining the alkali-zeolite with ammonium nitrate to produce an ion-exchanged zeolite; heating the ion-exchanged zeolite to form a protonated zeolite; and calcining the protonated zeolite to form the boron-silicalite-1. In embodiments, the method may include combining a templating agent, water, and boric acid in a first hydrothermal unit; heating the first microwave unit to form a boron-zeolite; calcining the boron-zeolite to form an alkali-zeolite; combining the alkali-zeolite with ammonium nitrate to produce an ion-exchanged zeolite; heating the ion-exchanged zeolite to form a protonated zeolite; and calcining the protonated zeolite to form the boron-silicalite-1. The boron-silicalite-1 may be microscale or nanoscale. 1. A method for the production of microscale boron-silicalite-1 , the method comprising:combining a mineralizer agent, a templating agent, water, a silica compound, and boric acid in a first microwave unit;heating the first microwave unit to form a boron-zeolite;calcining the boron-zeolite to form an alkali-zeolite;combining the alkali-zeolite with ammonium nitrate to produce an ion-exchanged zeolite;heating the ion-exchanged zeolite to form a protonated zeolite; andcalcining the protonated zeolite to form the microscale boron-silicalite-1;wherein the microscale boron-silicalite-1 has an average crystal size of from 1 micrometers to 5 micrometers when measured according to Scanning Electron Microscopy (SEM).2. The method of claim 1 , further comprising passing the alkali-zeolite to the first microwave unit claim 1 , and wherein combining the alkali-zeolite with ammonium nitrate and heating the ion-exchanged ...

STRUCTURED PHOTOCATALYST, STRUCTURED PHOTOCATALYST COMPOSITION, PHOTOCATALYST COATED MATERIAL, METHOD FOR PRODUCING STRUCTURED PHOTOCATALYST, AND METHOD FOR DECOMPOSING ALDEHYDES

An object of the present disclosure is to provide a structured photocatalyst that can effectively prevent aggregation of photocatalyst particles and maintain favorable photocatalytic functionality over a long period of time. A structured photocatalyst including a support of porous structure including a zeolite-type compound and at least one photocatalytic substance present in the support, the support including channels connecting with each other, and the photocatalytic substance including metal oxide nanoparticles and being present at least at the channels of the support. 1. A structured photocatalyst comprising:a support of porous structure including a zeolite-type compound; andat least one photocatalytic substance present in the support,the support including channels connecting with each other,the photocatalytic substance being metal oxide nanoparticles and being present at least at the channels of the support,the channels include an enlarged pore portion, andthe photocatalytic substance is present at least at the enlarged pore portion.2. The structured photocatalyst according to claim 1 , whereinthe enlarged pore portion causes a plurality of pores constituting any one of a one-dimensional pore, a two-dimensional pore, and a three-dimensional pore to connect with each other.3. The structured photocatalyst according to claim 1 , whereinthe metal oxide nanoparticles include titanium or an alloy oxide including titanium.4. The structured photocatalyst according to claim 1 , whereinthe metal oxide nanoparticles have an average particle diameter that is greater than an average inner diameter of the channels and not greater than an inner diameter of the enlarged pore portion.5. The structured photocatalyst according to claim 1 , whereinthe metal oxide nanoparticles include a metal element (M) in an amount from 0.5 mass % to 2.5 mass % with respect to the structured catalyst.6. The structured photocatalyst according to claim 1 , whereinthe metal oxide nanoparticles have ...

A COMPOSITION COMPRISING A ZEOLITIC MATERIAL SUPPORTED ON A SUPPORT MATERIAL

A composition comprising a support material which comprises silicon carbide on the surface of which a zeolitic material of the AEI/CHA family is supported, wherein at least 99 weight-% of the framework structure of the zeolitic material consist of a tetravalent element Y which is one or more of Si, Ge, Ti, Sn and V; a trivalent element X which is one or more of Al, Ga, In, and B; O; and H. 1. A composition , comprising a support material comprising silicon carbide ,wherein, on a surface of the support material, a zeolitic material of the AEI/CHA family is supported,wherein at least 99 weight-% of a framework structure of the zeolitic material consists of: a tetravalent element Y which is one or more of Si, Ge, Ti, Sn and V; a trivalent element X which is one or more of Al, Ga, In, and B; O; and H.2. The composition of claim 1 , wherein the silicon carbide comprised in the support material comprises one or more of alpha silicon carbide claim 1 , beta silicon carbide claim 1 , and gamma silicon carbide.3. The composition of claim 1 , wherein at least 50 weight % of the support material consists of silicon carbide claim 1 ,wherein the support material optionally further comprises one or more of elemental silicon and silica.4. The composition of claim 1 , wherein the zeolitic material of the AEI/CHA family is a zeolitic material having framework type AEI or having framework type CHA.5. The composition of claim 1 , wherein the zeolitic material of the AEI/CHA family is a zeolitic material having framework type CHA.6. The composition of claim 1 , having one or more of the following characteristics:{'sup': '2', 'a BET specific surface area in a range of from 100 to 300 m/g;'}{'sup': '2', 'a specific micropore surface area in a range of from 100 to 250 m/g;'}{'sup': '2', 'an external surface area in a range of from 2 to 10 m/g;'}{'sup': '3', 'a total pore volume in a range of from 0.05 to 0.20 cm/g;'}{'sup': '3', 'a micropore volume in a range of from 0.04 to 0.15 cm/g;'}{' ...

FUNCTIONAL STRUCTURAL BODY AND METHOD FOR MAKING FUNCTIONAL STRUCTURAL BODY

To provide a functional structural body that can realize ong life time by suppressing the decline in function of the functional substance and that can attempt to save resources without requiring a complicated replacement operation, and to provide a method for making the functional structural body. The functional structural body () includes a skeletal body () of a porous structure composed of a zeolite-type compound, and at least one functional substance () present in the skeletal body (), the skeletal body () has channels () connecting with each other, and the functional substance is present at least the channels () of the skeletal body (). 1. A functional structural body , comprising:a skeletal body of a porous structure composed of a zeolite-type compound; andat least one functional substance present in the skeletal body,wherein the skeletal body has channels connecting with each other, andthe functional substance is present at least in the channels of the skeletal body.2. The functional structural body according to claim 1 , wherein the channels have any one of a one-dimensional pore claim 1 , a two-dimensional pore claim 1 , and a three-dimensional pore defined by the framework of the zeolite-type compound and an enlarged pore portion which has a diameter different from that of any of the one-dimensional pore claim 1 , the two-dimensional pore claim 1 , and the three-dimensional pore claim 1 , andwherein the functional substance is present at least in the enlarged pore portion.3. The functional structural body according to claim 2 , wherein the diameter expanding portion causes a plurality of pores that constitute any one of the one-dimensional pore claim 2 , the two-dimensional pore claim 2 , and the three-dimensional pore to connect with each other.4. The functional structural body according to claim 1 , whereinthe functional substance is a catalytic substance; andthe skeletal body is a support that supports at least one catalytic substance.5. The functional ...

NOVEL ZEOLITE SYNTHESIS WITH ALKALINE EARTH METAL

Provided are a novel form of AFX zeolite, a novel synthesis technique for producing pure phase small pore zeolites, a novel synthesis method for producing a zeolite with an increased Al pair content, a catalyst comprising the AFX zeolite in combination with a metal, and methods of using the same. 1. An aluminosilicate zeolite comprising at least about 90% phase pure AFX framework , wherein the aluminosilicate zeolite has a short hexagonal prism morphology.2. The aluminosilicate zeolite of claim 1 , wherein the aluminosilicate zeolite is free or substantially free of alkaline metal.3. A method for making an aluminosilicate zeolite having a small pore framework comprising reacting a synthesis gel comprising at least one zeolite claim 1 , a structure directing agent claim 1 , an alkaline earth metal source claim 1 , and an optional silica source at a temperature of at least about 100° C. until crystals of the small pore zeolite form.4. The method of claim 3 , wherein the small pore zeolite crystals are at least about 90% phase pure.5. The method of claim 3 , wherein the synthesis gel is substantially free of alkaline metal.6. The method of claim 3 , wherein the synthesis gel has one or more of the following compositional molar ratios:{'sub': 2', '2', '3, 'SiO/AlOof about 10 to about 80;'}{'sub': 2', '2', '3, 'NaO/AlOof about 0 to about 2;'}{'sub': AE', '2', '3', 'AE, 'MO/AlOof about 0.3 to about 1.5 (Mcan be Ca, Sr, or Ba);'}{'sub': 2', '2', '3, 'SDAO/AlOof about 0.7 to about 20;'}{'sub': 2', '2', '3, 'HO/AlOof about 300 to about 3000; and'}{'sup': '−', 'sub': '2', 'OH/SiOof about 0.25 to about 0.5.'}7. The method of claim 3 , wherein the SDA cation is 1 claim 3 ,3-bis(1-adamantyl)imidazolium claim 3 , N claim 3 ,N-diethyl-cis 2 claim 3 ,6-dimethylpiperidinium claim 3 , N claim 3 ,N-dimethyl-3 claim 3 ,5-dimethylpiperidinium claim 3 , N claim 3 ,N claim 3 ,N-1-trimethyladamantylammonium claim 3 , or N claim 3 ,N claim 3 ,N-dimethylethylcyclohexylammonium.8. A catalyst ...

FUNCTIONAL STRUCTURAL BODY AND METHOD FOR MAKING FUNCTIONAL STRUCTURAL BODY

A functional structural body that can realize a prolonged life time by suppressing the decrease in function and that can fulfill resource saving without requiring a complicated replacement operation is provided. A functional structural body includes a skeletal body of a porous structure composed of a zeolite-type compound; and at least one solid acid present in the skeletal body, the skeletal body has channels connecting with each other, and the solid acid is present at least in the channels of the skeletal body. 1. A functional structural body , comprising:a skeletal body of a porous structure composed of a zeolite-type compound; andat least one solid acid present in the skeletal body,the skeletal body having channels connecting with each other,the solid acid being present at least in the channels of the skeletal body,the channel has an enlarged pore portion, andthe solid acid is at least embedded by the enlarged pore portion.2. The functional structural body according to claim 1 , wherein the enlarged pore portion causes a plurality of pores constituting any one of an one-dimensional pore claim 1 , a two-dimensional pore claim 1 , and a three-dimensional pore to connect with each other.3. The functional structural body according to claim 1 , wherein the solid acid is nanoparticles having a catalytic function claim 1 , and the skeletal body is a support that supports the solid acid.4. The functional structural body according to claim 3 , wherein an average particle size of the nanoparticles is greater than an average inner diameter of the channel and is less than or equal to an inner diameter of an enlarged pore portion.5. The functional structural body according to claim 3 , wherein the average particle size of the nanoparticles is from 0.1 nm to 50 nm.6. The functional structural body according to claim 5 , wherein the average particle size of the nanoparticles is from 0.45 nm to 14.0 nm.7. The functional structural body according to claim 3 , wherein a ratio of ...

PHOTOCATALYTIC COATED GRANULES AND METHOD OF MAKING SAME

These embodiments relate to a method of attaching photocatalytic materials to inorganic surfaces. A method is described wherein metal hydroxide is converted to metal oxide, creating metal oxide linkages to attach photocatalysts to an inorganic surface. The photocatalyst attached inorganic material is useful in products that can partially or fully oxidize certain volatile organic compounds from a gas or liquid stream. 1. A method for making a photocatalytically active composite film comprising:creating a metal hydroxide mixture by mixing a metal oxide or metalloid oxide with a fluid carrier;adding a photocatalytic compound to the metal hydroxide mixture; andconverting the metal hydroxide to metal oxide by heating a mixture containing the metal hydroxide, the fluid carrier and the photocatalytic compound at a temperature greater than 250° C.2. The method according to claim 1 , further comprising agitating the mixture containing the metal hydroxide claim 1 , the fluid carrier and the photocatalytic compound a time sufficient to interact the photocatalytic compound with the metal hydroxide.3. The method according to claim 1 , further comprising heating the mixture containing the metal hydroxide claim 1 , the fluid carrier and the photocatalytic compound a time sufficient to remove volatile components of the fluid carrier.4. The method according to claim 1 , wherein the metal hydroxide is selected from AlOand SiO.5. The method according to claim 1 , wherein the metal hydroxide is pumice.6. The method according to claim 1 , wherein the photocatalytic material comprises WOand/or TiO.7. The method according to claim 6 , wherein the photocatalytic material is WO.8. The method according to claim 5 , wherein the photocatalytic material comprises WOand Ceria.9. The method according to claim 1 , wherein the fluid carrier comprises water.10. The method according to claim 1 , further comprising washing the fused metal oxides.11. A photocatalytic composite made by the method .12. A ...

Preparation method of a visible-light-driven cc@sns2/sno2 composite catalyst, and application thereof

The present invention disclosed preparation method of a visible-light-driven CC@SnS 2 /SnO 2 composite catalyst, and application thereof, comprising the following steps: preparing CC@SnS 2 composite material in a solvent by using SnCl 4 .5H 2 O and C 2 H 5 NS as raw materials and carbon fiber cloth as a supporting material; calcining said CC@SnS 2 composite material to obtain the visible-light-driven CC@SnS 2 /SnO 2 composite catalyst. The present invention overcomes defects of the traditional methods of treating chromium-containing wastewater, including chemical precipitation, adsorption, ion exchange resin and electrolysis, and the photocatalytic technology can make full use of solar light source or artificial light source without adding adsorbent or reducing agent. In this case, the use of semiconductor photocatalyst to convert hexavalent chromium in chromium wastewater into less toxic and easily precipitated trivalent chromium greatly reduces the cost and energy consumption.

CATALYST MATERIALS, SYSTEMS, AND METHODS OF MAKING

Disclosed herein are catalyst materials and vehicle catalytic converters having platinum atomically dispersed on a ceria support and having a Tvalue less than or equal to 150° C., wherein the Tvalue represents the temperature required for 90% CO conversion. Also disclosed are methods of making the catalyst material involving hydrothermally treating at a temperature of at least 700° C. a Pt/ceria material comprising atomically dispersed Pt on a ceria support and activating 90% CO conversion at a temperature less than or equal to 150° C. (i.e., T≤150° C.). 1. A catalyst material comprising platinum atomically dispersed on an activated ceria support and having a Tvalue less than or equal to 150° C. , wherein the Tvalue represents the temperature required for 90% CO conversion.2. The catalyst material of claim 1 , wherein the activated ceria support comprises activated surface lattice oxygen sites.3. The catalyst material of claim 2 , wherein the activated surface lattice oxygen sites are proximal to the atomically dispersed platinum.4. The catalyst material of claim 2 , wherein the activated surface lattice oxygen sites are stable up to 800° C. in an oxidizing environment.5. The catalyst material of claim 1 , exhibiting a second reduction peak at temperature lower than a first reduction peak attributed to a Pt—O—Ce bond in a hydrogen temperature programmed reduction profile.6. The catalyst material of claim 1 , having no observable aggregates of platinum at the surface region of the catalyst material.7. The catalyst material of claim 1 , capable of maintaining 95% CO conversion for at least 300 hours at 145° C. for an exhaust stream having a gas hourly space velocity of 200 claim 1 ,000 ml per gram of the catalyst material and a CO/Omolar ratio of 1/25.8. The catalyst material of claim 1 , wherein the atomically dispersed platinum is covalently bonded to the activated ceria support.9. The catalyst material of claim 1 , further comprising Pt atomically dispersed on the ...

METHODS OF PRODUCING ISOMERIZATION CATALYSTS

Methods of producing an isomerization catalyst include preparing a catalyst precursor solution, hydrothermally treating the catalyst precursor solution to produce a magnesium oxide precipitant, and calcining the magnesium oxide precipitant to produce the isomerization catalyst. The catalyst precursor solution includes at least a magnesium precursor, a hydrolyzing agent, and polyethylene glycol. Methods of producing propene from a butene-containing feedstock with the isomerization catalyst and a metathesis catalyst are also disclosed. 1. A method of producing an isomerization catalyst , the method comprising:preparing a catalyst precursor solution comprising at least a magnesium precursor, a hydrolyzing agent, and polyethylene glycol;hydrothermally treating the catalyst precursor solution to produce a magnesium oxide precipitant; andcalcining the magnesium oxide precipitant to produce the isomerization catalyst.2. The method of claim 1 , where the molar ratio of the magnesium precursor to the hydrolyzing agent in the catalyst precursor solution is from 1:10 to 1:1.3. The method of claim 1 , where the molar ratio of the magnesium precursor to polyethylene glycol in the catalyst precursor solution is from 1:0.01 to 1:0.1.4. The method of claim 1 , further comprising adjusting the pH of the catalyst precursor solution.5. The method of claim 4 , where the pH of the catalyst precursor solution is adjusted to a pH of from 3 to 7.6. The method of claim 4 , where the pH of the catalyst precursor solution is adjusted to a pH of from 8 to 12.7. The method of claim 1 , where hydrothermally treating the catalyst precursor solution comprises heating the catalyst precursor solution to a temperature of from 100° C. to 140° C. for a duration of from 48 hours to 96 hours.8. An isomerization catalyst produced by the method of .9. The isomerization catalyst of claim 8 , where the surface area of the isomerization catalyst is from 125 m/g to 225 m/g.10. The isomerization catalyst of ...

SYNTHESIS OF MTW FRAMEWORK TYPE ZEOLITES VIA INTERZEOLITE TRANSFORMATION

A method is disclosed for synthesizing MTW framework type zeolites via interzeolite transformation in the presence of polyethyleneimine. 1. A method of synthesizing a MTW framework type zeolite , the method comprising: (1) a FAU framework type zeolite;', '(2) polyethyleneimine (Q);', '(3) fluoride ions; and', '(4) water; and, '(a) preparing a reaction mixture comprising(b) subjecting the reaction mixture to crystallization conditions sufficient to form crystals of the MTW framework type zeolite.4. The method of claim 1 , wherein the polyethyleneimine is a linear polyethyleneimine.5. The method of claim 4 , wherein the linear polyethyleneimine has a number average molecular weight in a range of 1500 to 5000.6. The method of claim 1 , wherein the crystallization conditions include a temperature of from 125° C. to 200° C.7. An MTW framework type zeolite comprising polyethyleneimine within its pore structure.10. The MTW framework type zeolite of claim 7 , wherein the polyethyleneimine is a linear polyethyleneimine.11. The MTW framework type of claim 10 , wherein the linear polyethyleneimine has a number average molecular weight in a range of 1500 to 5000. The present application claims priority from U.S. Provisional Patent Application No. 62/423,271, filed on Nov. 17, 2016, the disclosure of which is hereby incorporated by reference in its entirety.This disclosure relates generally to the synthesis of MTW framework type zeolites.Molecular sieves are a commercially important class of crystalline materials. They have distinct crystal structures with ordered pore structures which are demonstrated by distinct X-ray diffraction patterns. The crystal structure defines cavities and pores which are characteristic of the different species. Molecular sieves such as zeolites have been used extensively in catalysis, adsorption, separation, and chromatography.Molecular sieves identified by the International Zeolite Association as having the framework type MTW are known. Examples of ...

IRON-PROMOTED ZEOLITE AND CATALYST MADE THEREFROM

The present disclosure provides a method of forming a selective catalytic reduction (SCR) catalyst, the method including receiving a first iron-promoted zeolite having a first iron content, and treating the iron-promoted zeolite with additional iron in an ion exchange step to form a second iron-promoted zeolite with a second iron content, the second iron content being higher than the first iron content. A selective catalytic reduction (SCR) catalyst composition including an ironpromoted zeolite having at least about 6 weight percent iron, based on total weight of the ironpromoted zeolite, wherein the iron content of the zeolite was added to the zeolite in at least two separate steps is also provided herein. 1. A method of forming a selective catalytic reduction (SCR) catalyst , the method comprising:receiving a first iron-promoted zeolite having a first iron content; andtreating the iron-promoted zeolite with additional iron in an ion exchange step to form a second iron-promoted zeolite with a second iron content, the second iron content being higher than the first iron content.2. The method of claim 1 , wherein the first iron content is from about 2 to about 8 wt % and the second iron content is about 6 to about 10 wt % claim 1 , based on the total weight of the iron-promoted zeolite.3. The method of claim 1 , wherein the second iron content is at least about 15% greater than the first iron content claim 1 , more particularly at least about 20% higher.4. The method of claim 1 , wherein the iron-promoted zeolite is a zeolitic material having a BEA framework structure.5. The method of claim 4 , wherein the zeolitic material having a BEA framework structure is obtained from an organo-template-free synthetic process.6. The method of claim 1 , wherein the iron-promoted zeolite has a silica-to-alumina molar ratio (SAR) of about 10 or less.7. The method of claim 1 , wherein the iron-promoted zeolite has a silica-to-alumina molar ratio (SAR) of about 5 or less.8. The ...

AMORPHOUS CALCIUM PHOSPHATE CATALYST FOR USE IN PRODUCTION OF 1,3-BUTADIENE AND METHYL ETHYL KETONE FROM 2,3-BUTANEDIOL, AND METHOD OF PREPARING THE SAME

Disclosed are an amorphous calcium phosphate catalyst for use in production of 1,3-butadiene and methyl ethyl ketone from 2,3-butanediol, a preparation method thereof and a method of producing 1,3-butadiene and methyl ethyl ketone from 2,3-butanediol using the amorphous calcium phosphate catalyst. 1. A method of preparing an amorphous calcium phosphate catalyst for use in production of 1 ,3-butadiene and methyl ethyl ketone from 2 ,3-butanediol , comprising:(a) reacting a phosphoric acid-containing solution with an alkali, thus preparing a phosphoric acid-alkali aqueous solution;(b) adding the phosphoric acid-alkali aqueous solution with a calcium precursor aqueous solution, thus preparing a calcium phosphate slurry; and(c) thermally treating the slurry, thus obtaining an amorphous calcium phosphate catalyst.2. The method of claim 1 , wherein in (a) claim 1 , the phosphoric acid-containing solution comprises at least one selected from the group consisting of orthophosphoric acid (HPO) claim 1 , pyrophosphoric acid (HPO) claim 1 , tripolyphosphoric acid (HPO) claim 1 , and tetrapolyphosphoric acid (HPO).3. The method of claim 1 , wherein preparing the calcium phosphate shiny in (b) is performed at a pH of higher than 5.0 but less than 11.0.4. The method of claim 1 , wherein in (b) claim 1 , a Ca/P ratio is 1.20-1.67.5. The method of claim 1 , wherein in (b) claim 1 , a Ca/P ratio is 1.20-1.30.6. The method of claim 1 , wherein in (b) claim 1 , the calcium precursor comprises at least one selected from the group consisting of calcium acetate (Ca(CHCOO)) claim 1 , calcium nitrate (Ca(NO)) claim 1 , and calcium chloride (CaCl).7. The method of claim 1 , wherein thermally treating in (c) is performed at 400-600° C. for 1-10 hr.8. An amorphous calcium phosphate catalyst for use in production of 1 claim 1 ,3-butadiene and methyl ethyl ketone from 2 claim 1 ,3-butanediol.9. The amorphous calcium phosphate catalyst of claim 8 , which has a Ca/P ratio of 1.20-1.67.10. The ...

ZEOLITE, AND PRODUCTION METHOD AND USE THEREFOR

The present invention provides a novel high-silica zeolite having a high molar ration of a tetravalent element (Y) to a trivalent element (X) in terms of oxide. 1. A zeolite , comprising a trivalent element X and a tetravalent element Y , wherein a molar ratio n=YO/XOin terms of oxide is 9.5 or more , and the zeolite comprises an RHO-type structure.2. A zeolite , comprising a trivalent element X and a tetravalent element Y , wherein a molar ratio n=YO/XOin terms of oxide is 9.5 or more , and the zeolite has at least lattice spacings d (Å) , detected in a measurement by powder X-ray diffractometry , of: 10.58±0.40 , 6.10±0.30 , 5.28±0.20 , 4.73±0.30 , 4.32±0.10 , 4.00±0.20 , 3.52±0.10 , and 3.34±0.10.3. The zeolite according to claim 1 , further comprising a template Q claim 1 , wherein a molar ratio m=Q/XOis more than 0 and less than 6.4. The zeolite according to claim 1 , wherein X comprises aluminum.5. The zeolite according to claim 1 , wherein Y comprises silicon.6. The zeolite according to claim 1 , further comprising another metal element.7. The zeolite according to claim 6 , wherein the other metal element is iron and/or copper.8. The zeolite according to claim 6 , wherein a content of the other metal element is 0.5% to 10% by weight in a total amount of the zeolite under an anhydrous state.9. A catalyst claim 1 , comprising the zeolite according to .10. An exhaust gas treatment catalyst claim 1 , comprising the zeolite according to .11. The exhaust gas treatment catalyst according to claim 10 , wherein the exhaust gas treatment catalyst is a selective reduction catalyst suitable for an exhaust gas comprising a nitrogen oxide.12. A method for producing a zeolite claim 10 , comprising performing hydrothermal synthesis of a zeolite from an aqueous gel that is prepared by adding a mixed solution comprising a crown ether claim 10 , an alkali claim 10 , and water to a solution comprising an aluminum atom material claim 10 , and by then dropwise adding a liquid ...

SELECTIVE HYDROGENATION CATALYST FOR C3 HYDROCARBON CUTS FROM STEAM CRACKING AND/OR CATALYTIC CRACKING

A catalyst comprises an active phase constituted by palladium, and a porous support comprising at least one refractory oxide selected from the group constituted by silica, alumina and silica-alumina, in which: 1. A catalyst comprising an active phase constituted by palladium , and a porous support comprising at least one refractory oxide selected from the group constituted by silica , alumina and silica-alumina , in which:the palladium content in the catalyst is in the range 0.0025% to 1% by weight with respect to the total weight of catalyst;at least 80% by weight of the palladium is distributed in a crust at the periphery of the porous support, the thickness of said crust being in the range 25 to 500 μm;{'sup': '2', 'the specific surface area of the porous support is in the range 1 to 50 m/g;'}the metallic dispersion D of the palladium is less than 20%.2. The catalyst as claimed in claim 1 , in which the metallic dispersion D of the palladium is 18% or less.3. The catalyst as claimed in claim 1 , in which the palladium content in the catalyst is in the range 0.025% to 0.8% by weight with respect to the total weight of catalyst.4. The catalyst as claimed in claim 1 , characterized in that the specific surface area of the porous support is in the range 1 to 40 m/g.5. The catalyst as claimed in claim 1 , characterized in that at least 80% by weight of the palladium is distributed in a crust at the periphery of the porous support claim 1 , the thickness of said crust being in the range 50 to 450 μm.6. The catalyst as claimed in claim 1 , characterized in that the porous support is alumina.7. The catalyst as claimed in claim 1 , characterized in that the total pore volume of the support is in the range 0.1 to 1.5 cm/g.8. The catalyst as claimed in claim 1 , characterized in that the porous support comprises in the range 0.0050% to 0.25% by weight of sulphur with respect to the total weight of catalyst.9. The catalyst as claimed in claim 1 , characterized in that the ...

Modified Y-type molecular sieve, catalytic cracking catalyst comprising the same, their preparation and application thereof

A modified Y-type molecular sieve has a rare earth content of about 4% to about 11% by weight on the basis of the oxide, a phosphorus content of about 0.05% to about 10% by weight on the basis of PO, a sodium content of no more than about 0.5% by weight on the basis of sodium oxide, and an active element content of about 0.1% to about 5% by weight on the basis of the oxide, with the active element being gallium and/or boron. The modified Y-type molecular sieve has a total pore volume of about 0.36 mL/g to about 0.48 mL/g, a percentage of the pore volume of secondary pores having a pore size of 2-100 nm of about 20% to about 40%; a lattice constant of about 2.440 nm to about 2.455 nm, and a lattice collapse temperature of not lower than about 1060° C. 1. A modified Y-type molecular sieve , having a rare earth content of about 4% to about 11% by weight on the basis of the oxide , a phosphorus content of about 0.05% to about 10% by weight on the basis of PO , a sodium content of no more than about 0.5% by weight on the basis of sodium oxide , and an active element content of about 0.1% to about 5% by weight on the basis of the oxide , with the active element being gallium and/or boron , based on the weight of the modified Y-type molecular sieve on a dry basis;wherein the modified Y-type molecular sieve has a total pore volume of about 0.36 mL/g to about 0.48 mL/g, a percentage of the pore volume of secondary pores having a pore size of 2-100 nm to the total pore volume of about 20% to about 40%;a lattice constant of about 2.440 nm to about 2.455 nm, a lattice collapse temperature of not lower than about 1060° C., a percentage of non-framework aluminum content to the total aluminum content of no more than about 10%, and a ratio of B acid to L acid in the strong acid content of the modified Y-type molecular sieve of no less than about 3.5.2. The modified Y-type molecular sieve according to claim 1 , wherein the modified Y-type molecular sieve has one or more of the ...

ALUMINOPHOSPHATE MOLECULAR SIEVES USING AN ORGANO-1-OXA-4-AZONIUMCYCLOHEXANE COMPOUND

A method for synthesizing an aluminophosphate based molecular sieve is described. The method may include the steps of: (a) preparing an aqueous mixture comprising water, a substituted hydrocarbon, and a 1-oxa-4-azacyclohexane derivative; (b) reacting the aqueous mixture; (c) obtaining a solution comprising an organo-1-oxa-4-azoniumcyclohexane compound; (d) forming a reaction mixture comprising reactive sources of Al, and P, and the solution; and (e) heating the reaction mixture to form the molecular sieve. 1. A method for synthesizing an aluminophosphate based molecular sieve comprising:(a) preparing an aqueous mixture comprising water, a substituted hydrocarbon, and a 1-oxa-4-azacyclohexane derivative;(b) reacting the aqueous mixture;(c) obtaining a solution comprising an organo-1-oxa-4-azoniumcyclohexane compound;(d) forming a reaction mixture comprising reactive sources of Al, and P, and the solution; and(e) heating the reaction mixture to form the molecular sieve.2. The method of claim 1 , wherein the step of reacting the aqueous mixture occurs at a temperature between 20° C. and 100° C.3. The method of claim 1 , wherein the organo-1-oxa-4-azoniumcyclohexane compound is a structure directing agent.4. The method of wherein the substituted hydrocarbon is a halogen substituted alkane selected from the group consisting of bromoethane claim 1 , iodoethane claim 1 , chloropropane claim 1 , bromopropane claim 1 , iodopropane claim 1 , chlorobutane claim 1 , 1-bromobutane claim 1 , 2-bromobutane claim 1 , iodobutane claim 1 , 1-bromo-2-methylpropane claim 1 , 2-bromo-2-methylpropane claim 1 , chloropentane claim 1 , bromopentane claim 1 , iodopentane claim 1 , 2-bromopentane claim 1 , chlorohexane claim 1 , bromohexane claim 1 , iodohexane claim 1 , benzyl halide claim 1 , 1-chloro-2-phenylethane claim 1 , 1-bromo-2-phenylethane claim 1 , 1-iodo-2-phenylethane claim 1 , 1-halomethane naphthalene claim 1 , 2-halomethane naphthalene claim 1 , and halo-substituted non- ...

A METHOD OF SYNTHESISING A PT(II) COMPLEX; A PT(II) COMPLEX; USE OF SUCH A COMPLEX AS A PHOTOACTIVATABLE CATALYST IN A HYDROSILYLATION REACTION

A method of synthesising a Pt(II) complex includes a first step of preparing a reaction mixture comprising a water-soluble hexachloroplatinate salt and a compound according to Formula I′, or salt thereof, and allowing the water-soluble hexachloroplatinate salt and the compound according to Formula I′ to react and a second step of adding a further quantity of the compound according to Formula I′, or a salt thereof, to the reaction mixture. Products of this method are Pt(II) complexes according to Formula I The Pt(II) complexes are useful as catalysts in hydrosilylation reactions. 2. The method of claim 1 , further comprising an intermediate step claim 1 , after the first step but before the second step claim 1 , of adding a reducing agent to the reaction mixture.3. The method of claim 1 , wherein in the first step the compound according to Formula I′ is used in stoichiometric excess.4. The method of claim 1 , wherein in the first step the reaction mixture further comprises a solvent selected from water or water mixed with an alcohol.57-. (canceled)8. The method of claim 1 , wherein the water-soluble hexachloroplatinate salt is selected from Na[PtCl] and chloroplatinic acid.9. The method of claim 1 , wherein the first step further comprises leaving the reaction mixture to react for at least 10 minutes before any further step is carried out.10. (canceled)11. The method of claim 1 , wherein the compound according to Formula I′ and the water-soluble hexachloroplatinate salt are added to the reaction mixture in the first step in a molar ratio of at least 2:1.12. The method of claim 2 , wherein the reducing agent added in the intermediate step is an alcoholic reducing agent.13. The method of claim 2 , wherein the intermediate step comprises heating the reaction mixture to a temperature of at least 50° C. and allowing the mixture to remain at this temperature for at least 2 hours.1415-. (canceled)16. The method of claim 1 , wherein Y and Z claim 1 , together with the two ...

METATITANIC ACID PARTICLE, COMPOSITION FOR FORMING PHOTOCATALYST, AND PHOTOCATALYST

A metatitanic acid particle includes a metal having a hydrocarbon group, which is bonded to a surface of the metatitanic acid particle through an oxygen atom, and absorbs light having a wavelength of 450 nm and light having a wavelength of 750 nm, wherein an element ratio C/Ti between carbon C and titanium Ti in a surface of the metatitanic acid particle is from 0.3 to 1.2, and a reduced amount of C/Ti on the surface of the metatitanic acid particle before and after irradiation with an ultraviolet ray having a wavelength of 352 nm and at an irradiation intensity of 1.3 mW/cmfor 20 hours is from 0.1 to 0.9. 1. A metatitanic acid particle ,which comprises a metal having a hydrocarbon group, which is bonded to a surface of the metatitanic acid particle through an oxygen atom, andabsorbs light having a wavelength of 450 nm and light having a wavelength of 750 nm,wherein an element ratio C/Ti between carbon C and titanium Ti in a surface of the metatitanic acid particle is from 0.3 to 1.2, and{'sup': '2', 'a reduced amount of C/Ti on the surface of the metatitanic acid particle before and after irradiation with an ultraviolet ray having a wavelength of 352 nm and at an irradiation intensity of 1.3 mW/cmfor 20 hours is from 0.1 to 0.9.'}2. The metatitanic acid particle according to claim 1 ,which has an absorption in a whole range of a wavelength of 400 nm to 800 nm in the visible absorption spectrum.3. The metatitanic acid particle according to claim 1 ,{'sup': 1', '2', '1', '2', '1', '2, 'sub': n', 'm, 'wherein the metal having a hydrocarbon group is derived from a compound represented by RMRwherein Rrepresents an aliphatic hydrocarbon group or an aromatic hydrocarbon group, which is saturated or unsaturated and has 1 to 20 carbon atoms, Rrepresents a halogen atom or an alkoxy group, M represents a metal atom, n represents an integer of 1 to 3, and m represents an integer of 1 to 3, provided that n+m=4 is satisfied, in a case where n represents an integer of 2 or 3, ...

METHOD FOR PREPARING SILICATE/CARBON COMPOSITE FROM ATTAPULGITE, AND USE OF SILICATE/CARBON COMPOSITE

A method for preparing a silicate/carbon composite from attapulgite, and use of the silicate/carbon composite are disclosed. The preparation method includes: (1) with attapulgite as a raw material, preparing SiOwith a special structure; (2) dispersing the prepared SiOin water to obtain a suspension, and subjecting the suspension to ultrasonic dispersion; dissolving a metal nitrate in the suspension, adding NHCl, and adding ammonia water dropwise to the suspension; and adding sucrose to obtain a suspension; (3) subjecting the suspension to microwave hydrothermal reaction; after the reaction is completed, centrifuging a resulting system; and separating a resulting solid; and (4) subjecting the solid to high-temperature calcination in a muffle furnace, and grinding a resulting product to obtain the silicate/carbon composite, which can be used in photocatalytic ammonia synthesis. 1. A method for preparing a silicate/carbon composite from attapulgite , wherein the silicate/carbon composite has a general formula: xMSiO/C , wherein a molar ratio of MSiOto C is x , and a range of the x is 0.1 to 0.3 , and the metal M is one selected from the group consisting of Fe , Co , and Ni; andthe method for preparing the silicate/carbon composite comprises the following steps:{'sub': '2', '(1) mixing an attapulgite powder with ammonium sulfate in a ceramic crucible to obtain a first resulting mixture, putting the ceramic crucible in a muffle furnace for a calcination and heating and calcining the first resulting mixture to obtain a calcination product; after the calcination, naturally cooling the calcination product to room temperature; dispersing the calcination product in a hydrochloric acid solution to obtain a second resulting mixture, and conducting a water bath heating reaction on the second resulting mixture under a stirring to obtain a first resulting solid; and separating, washing, and drying the first resulting solid to obtain SiOwith a special structure;'}{'sub': 2', '2', ' ...

SLURRY COMPOSITION FOR CATALYST AND METHOD FOR PRODUCING SAME, METHOD FOR PRODUCING CATALYST USING THIS SLURRY COMPOSITION FOR CATALYST, AND METHOD FOR PRODUCING CU-CONTAINING ZEOLITE

A slurry composition for a catalyst and a method for producing the same, a catalyst and a method for producing the same using the slurry composition for a catalyst. The method omits many heretofore required treatment steps and reduces catalyst production cost. The method comprising the steps of providing a slurry composition for a catalyst, comprising at least an aluminosilicate, Cu, and water, and having a solid concentration of 0.1% by mass to 90% by mass, wherein a component for a catalyst has composition represented by AlO.xSiO.yTO.zCuO (wherein T is a quaternary ammonium cation, and x, y and z are numbers that satisfy 10≤x≤40, 0.1≤y<2.0, and 0.1≤z<2.0, respectively) in terms of molar ratio based on an oxide; coating at least one side of a support with this slurry composition; and heat-treating at 350° C. or higher. 1. A slurry composition for a catalyst ,comprising at least an aluminosilicate, Cu, and water, andhaving a solid concentration of 0.1% by mass to 90% by mass, wherein{'sub': 2', '3', '2', '2, 'a component for a catalyst has composition represented by AlO.xSiO.yTO.zCuO (wherein T is a quaternary ammonium cation, and x, y and z are numbers that satisfy 10≤x≤40, 0.1≤y<2.0, and 0.1≤z<2.0, respectively) in terms of molar ratio based on an oxide.'}2. The slurry composition for a catalyst according to claim 1 , further comprising 0.1 to 40% by mass of a binder.3. The slurry composition for a catalyst according to claim 1 , wherein{'sup': 1', '2', '1', '2', '2, 'sub': '3', 'the T is a quaternary ammonium cation represented by the general formula RN(R)wherein Rrepresents a linear, branched or cyclic hydrocarbon group having 1 or more and 12 or less carbon atoms, wherein the hydrocarbon group optionally contains a heteroatom and optionally contains a substituent, Rrepresents a linear or branched alkyl group having 1 or more and 4 or less carbon atoms, and a plurality of Rare the same as or different from each other.'}4. The slurry composition for a catalyst ...

METHOD OF SYNTHESIS OF NANO-SIZED BETA ZEOLITES CONTAINING MESOPORES AND USES THEREOF

Provided here are nano-sized mesoporous zeolite compositions and the methods of synthesis and use of these compositions. These nano-sized mesoporous zeolite compositions are synthesized from a mixture of silicon source and an aluminum source fumed or colloidal silica with aluminum powder or aluminum oxide. Also provided are methods for hydrocracking a hydrocarbon feedstock by using catalysts containing the nano-sized mesoporous zeolite composition. 1. A method for synthesizing a nano-sized mesoporous zeolite composition , the method comprising:mixing silica, a source of aluminum, and tetraethylammonium hydroxide to form an aluminosilicate fluid gel;drying the aluminosilicate fluid gel to form a dried gel mixture;subjecting the dried gel mixture to hydrothermal treatment to produce a zeolite precursor;adding cetyltrimethylammonium bromide (CTAB) to the zeolite precursor to form a templated mixture;subjecting the templated mixture to hydrothermal treatment to prepare a CTAB-templated zeolite;washing the CTAB-templated zeolite with distilled water;separating the CTAB-templated zeolite by centrifugation; anddrying and calcining the CTAB-templated zeolites to produce a nano-sized mesoporous zeolite composition.2. The method of claim 1 , wherein the silica is fumed silica.3. The method of claim 1 , wherein the silica is colloidal silica.4. The method of claim 1 , wherein the source of aluminum is aluminum oxide.5. The method of claim 1 , wherein the source of aluminum is aluminum powder.6. The method of claim 1 , wherein the dried gel mixture is subject to hydrothermal treatment in an autoclave at a temperature ranging from 100° C. to 150° C. to produce a zeolite precursor.7. The method of claim 6 , wherein the dried gel mixture is subject to hydrothermal treatment under constant rotation to produce a zeolite precursor.8. The method of claim 1 , wherein the zeolite composition is a mesoporous beta zeolite in a proton form.9. The method of claim 1 , wherein the zeolite ...

COHERENTLY GROWN COMPOSITE ALUMINOPHOSPHATE AND SILICOALUMINOPHOSPHATE MOLECULAR SIEVES

Coherently grown composites of two zeotypes are described. The coherently grown composites have a crystalline three-dimensional framework of at least AlOand POtetrahedral units. The two zeotypes are selected from the group consisting of AFX, LEV, CHA, and ERI. Methods of making the coherently grown composites are also described. 1. A coherently grown composite of two zeotypes having a crystalline three-dimensional framework of at least AlOand POtetrahedral units , the two zeotypes selected from the group consisting of AFX , LEV , CHA , and ERI.3. The coherently grown composite of wherein the two zeotypes are AFX and LEV.5. The coherently grown composite of wherein the two zeotypes are CHA and LEV.7. The coherently grown composite of wherein the two zeotypes are CHA and AFX.9. The coherently grown composite of wherein the composite comprises greater than 0 and less than 100 wt. % the first zeotype and less than 100 wt. % and greater than 0 wt. % of the second zeotype.10. The coherently grown composite of wherein the composite comprises greater than 5 and less than 95 wt. % the first zeotype and less than 95 wt. % and greater than 5 wt. % of the second zeotype.11. The coherently grown composite of wherein the composite comprises greater than 10 and less than 90 wt. % the first zeotype and less than 90 wt. % and greater than 10 wt. % of the second zeotype.12. The coherently grown composite of wherein the coherently grown composite comprises regions of the first zeotype and regions of the second zeotype that are coherently aligned so that an [010] zone axis of the first zeotype is parallel to an [010] zone axis of the second zeotype.13. The coherently grown composite of wherein R comprises a 1-oxa-4-azonium cyclohexane salt having the structure of Formula 1:{'br': None, 'sub': 9', '1', '2', '3', '4', '5', '6', '7', '8', '10, 'sup': 2+', '−, '[bis-N,N′-diR-(2,2′-diR-2,2′-diR-3,3′-diR-3,3′-diR-5,5′-diR-5,5′-diR-6,6′-diR-6,6′-diR-1,1′-oxa-4,4′-azonium cyclohexane)-R]2X ...

PROCESS FOR THE CONVERSION OF SUGARS TO LACTIC ACID AND 2-HYDROXY-3-BUTENOIC ACID OR ESTERS THEREOF COMPRISING A METALLO-SILICATE MATERIAL AND A METAL ION

A process for the preparation of lactic acid and 2-hydroxy-3-butenoic acid or esters thereof from a sugar in the presence of a metallo-silicate material, a metal ion and a solvent, wherein the metal ion is selected from one or more of the group consisting of potassium ions, sodium ions, lithium ions, rubidium ions and caesium ions. 1. A metallo-silicate material suitable for preparing lactic acid and 2-hydroxy-3-butenoic acid or esters thereof from a sugar , which metallo-silicate material comprises a metal ion selected from the group consisting of alkaline earth metal ions and alkali metal ions.2. The metallo-silicate material according to claim 1 , wherein the metallo-silicate material comprises a silicon oxide structure and an active metal and wherein the silicon oxide structure comprises M-O—Si bonds.3. The metallo-silicate material according to claim 1 , wherein the metallo-silicate material is a zeotype material.4. The metallo-silicate material according to claim 1 , wherein the metallo-silicate material is a non-crystalline material.5. The metallo-silicate material according to claim 1 , comprising a framework structure selected from the group consisting of BEA claim 1 , MFI claim 1 , FAU claim 1 , MOR claim 1 , FER claim 1 , MCM-41 and SBA-15.6. The metallo-silicate material according to claim 2 , wherein the active metal is selected from one or more of the group consisting of Sn claim 2 , Ti claim 2 , Pb claim 2 , Zr claim 2 , Ge and Hf.7. The metallo-silicate material according to claim 1 , selected from the group consisting of Sn-BEA claim 1 , Sn-MFI claim 1 , Sn-FAU claim 1 , Sn-MOR claim 1 , Sn-FER claim 1 , Sn-MCM-41 and Sn-SBA-15.8. The metallo-silicate material according to claim 2 , wherein the atomic ratio of silicon to active metal is in the range of from 50:1 to 1:400.9. The metallo-silicate material according to claim 2 , wherein the atomic ratio of silicon to active metal is in the range of from 75:1 to 1:300.10. The metallo-silicate material ...

PROCESS FOR PREPARING ZEOLITE BETA AND USE THEREOF

Method for preparing zeolite beta which method comprises crystallization of zeolite beta from a solution comprising a template, a silicon source and an aluminum source in which the template is polymeric compound comprising ionizable polydiallyldimethylammonium (PDADMA) cationcrystallization. Furthermore, the present invention provides the use of thus prepared zeolite beta in catalysts for hydrocarbon conversions. 1. A method for preparing zeolite beta which method comprises crystallization of zeolite beta from a solution comprising a template , a silicon source and an aluminum source in which the template is polymeric compound comprising ionizable polydiallyldimethylammonium (PDADMA) cation.2. A method according to claim 1 , wherein the zeolite beta is prepared by hydrothermal crystallization of a solution comprising PDADMA and a silicon source which are present in a molar ratio SiO/PDADMA between the silicon source calculated as SiOand the polymeric compound calculated as the cationic PDADMA monomer is 1-10 claim 1 , the molar ratio SiO/MO between the silicon source calculated as SiOand the base source calculated as alkali metal oxide MO is of 1-10.3. A method according to claim 1 , wherein the hydrothermal crystallization is carried out at a temperature of 150-230° C.4. The method of claim 1 , wherein the molar ratio SiO/AlObetween the silicon source calculated as SiOand the aluminum source calculated as AlOis of 20-100 claim 1 , preferably of 30-80.5. The method of claim 1 , comprising dissolving the aluminum source and the base source in the water claim 1 , adding the polymeric PDADMA compound and stirring for a time period of 0.2-1.5 h.6. The method of claim 1 , wherein the product obtained by crystallization is filtered claim 1 , dried and calcined sequentially to obtain a final zeolite beta with a composite pore structure.7. The method of claim 1 , wherein the templating polymeric PDADMA compound has a molecular weight of 1×10-5×10.8. The method of claim 1 , ...

HYBRID SAPO-34/ZSM-5 CATALYST, ITS PREPARATION AND ITS USE

Prepare a hybrid SAPO-34/ZSM-5 catalyst via sequential steps as follows: a) form a mixture consisting essentially of ZSM-5 as a sole source of silicon atoms, aluminum isopropoxide and a solution of orthophosphoric acid; b) combine the mixture with an aqueous solution of tetraethylammonium hydroxide to form a reaction mixture; and c) subject the reaction mixture to hydrothermal conditions for a period of time sufficient to convert the reaction mixture to a hybrid SAPO-34/ZSM-5 catalyst. Use the hybrid catalyst in converting an oxygenate (methanol and/or dimethyl ether) to an olefin. 1. A process for preparing a hybrid SAPO-34/ZSM-5 catalyst that comprises sequential steps as follows: a) forming a mixture consisting essentially of ZSM-5 as a sole source of silicon atoms , aluminum isopropoxide and a solution of orthophosphoric acid; b) combining the mixture with an aqueous solution of tetraethylammonium hydroxide to form a reaction mixture; and c) subjecting the reaction mixture to hydrothermal conditions for a period of time sufficient to convert the reaction mixture to a hybrid SAPO-34/ZSM-5 catalyst , the hydrothermal conditions comprising a temperature within a range of from 190 degrees centigrade (° C.) to 210° C. and autogenous pressure.2. The process of claim 1 , wherein ZSM-5 is present in a weight ratio of SAPO-34 to ZSM-5 within a range of from 96:4 to 85:15.3. The process of claim 1 , wherein ZSM-5 is present in a weight ratio of SAPO-34 to ZSM-5 within a range of from 94:6 to 90:10.4. The process of claim 1 , further comprising a sequential step d) that follows step c) wherein the hybrid SAPO-34/ZSM-5 catalyst undergoes calcination in an oxygen-containing atmosphere at a temperature within a range of from 550° C. to 650° C. for a period of time within a range of from one hour to 12 hours.5. A process for converting an oxygenate feedstream that comprises methanol and dimethyl ether to at least one olefin comprising placing the oxygenate in operative contact ...

METHOD FOR PRODUCING TRANSITION-METAL-CONTAINING ZEOLITE, TRANSITION METAL ZEOLITE PRODUCED BY THE METHOD, AND EXHAUST GAS PURIFICATION CATALYST INCLUDING THE ZEOLITE

Provided is a method for producing a transition-metal-containing silicoaluminophosphate that is highly suitable as a catalyst or an adsorbent and has excellent high-temperature hydrothermal durability and excellent water resistance, that is, excellent durability against water submersion (water-submersion durability), in a simple and efficient manner. A method for producing a transition-metal-containing zeolite, the method comprising a steam treatment step in which a transition-metal-containing zeolite is stirred at 710° C. or more and 890° C. or less in the presence of water vapor, the transition-metal-containing zeolite containing a transition metal in a zeolite having a framework structure including silicon atoms, phosphorus atoms, and aluminium atoms. 1. A method for producing a transition-metal-containing zeolite , the method comprising steam treating a transition-metal-containing zeolite by stirring the zeoltie at a temperature of 710° C. to 890° C. in the presence of water vapor , wherein the transition-metal-containing zeolite comprises a transition metal in a zeolite comprising at least silicon atoms , phosphorus atoms , and aluminum atoms in a framework structure2. The method of . wherein the steam treating. is performed at a temperature of 750° C. to 850° C.3. The method of claim 1 , wherein the transition metal comprises copper.4. The method of claim 1 , wherein the steam treating is performed in an atmosphere having a water vapor concentration of 1% by volume or more.5. The method of claim 1 , wherein the steam treating is performed for a time of 0.1 to 72 hours.6. The method of claim 1 , wherein the transition-metal-containing zeolite is stirred by using at least one selected from the group consisting of a stirrer having an axis claim 1 , a stirrer that does not have an axis claim 1 , a stirrer connected to a tank claim 1 , and a fluid.7. The method of claim 1 , wherein a content of the transition metal in the transition-metal-containing zeolite is 0.1% ...

SCR-Active Material Having Enhanced Thermal Stability

The invention relates to an SCR-active material, comprising a small-pore zeolite of the structure type levyne (LEV), aluminum oxide, and copper, characterized in that, based on the total material, the material contains 4 to 25 wt % of aluminum oxide. 1. An SCR-active material comprising(i) a small-pore zeolite of the levyne (LEV) structure type,(ii) aluminum oxide, and(iii) copper,wherein the copper is present in a first concentration on the aluminum oxide and in a second concentration on the small-pore zeolite,wherein it contains 4 to 25 wt % aluminum oxide, relative to the total SCR-active material.2. The SCR-active material according to claim 1 , wherein it contains 6 to 16 wt % aluminum oxide claim 1 , relative to the total SCR-active material.3. The SCR-active material according to claim 1 , wherein the total amount of copper claim 1 , calculated as CuO and relative to the total SCR-active material claim 1 , is 0.5 to 15 wt %.4. The SCR-active material according to claim 1 , wherein the small-pore zeolite of the levyne (LEV) structure type is an aluminosilicate.5. The SCR-active material according to claim 4 , wherein the small-pore zeolite of the levyne (LEV) structure type has an SAR value of 5 to 50.6. The SCR-active material according to claim 1 , wherein the small-pore zeolite of the levyne (LEV) structure type is a silicoaluminosilicate or an aluminophosphate.7. The SCR-active material according to claim 1 , wherein the atomic ratio of copper exchanged in the zeolite to skeleton aluminum in the zeolite is 0.25 to 0.6.8. The SCR-active material according to claim 1 , wherein the average crystallite size (d) of the small-pore zeolite of the levyne (LEV) structure type is 0.1 to 20 μm.9. The SCR-active material according to claim 1 , wherein the small-pore zeolite of the levyne (LEV) structure type forms a core claim 1 , and the aluminum oxide forms a shell surrounding this core.10. The SCR-active material according to claim 1 , wherein its specific surface ...

Hydrogenation Catalyst, Its Method of Preparation and Use

A method of preparing a hydrogenation catalyst, for example, a phthalate hydrogenation catalyst, comprising contacting a silica support having a median pore size of at least about 10 nm with a silylating agent to form an at least partially coated silica support, calcining said coated silica support to form a treated silica support, and depositing a noble metal, preferably ruthenium, on the treated silica support, and optionally contacting the treated silica support with an optional chelating agent to form the hydrogenation catalyst; a hydrogenation catalyst prepared by that method; and a method of hydrogenating unsaturated hydrocarbons, such as phthalates, in which an unsaturated hydrocarbon is contacted with hydrogen gas in the presence of the hydrogenation catalyst of the invention. 123.-. (canceled)24. A method for the preparation of a silica-supported noble metal hydrogenation catalyst comprising the steps of:(a) providing a silica support having a median pore size of at least about 10 nm;(b) steam treating said silica support to increase the hydroxyl concentration on the surface of said silica support after streaming to produce a steamed silica support;(c) contacting said streamed silica support with a silylating agent to coat at least part of said streamed silica support to produce a coated silica support;(d) calcining said coated silica support obtained in step (c) to produce a treated and coated silica support; and(e) dispersing a noble metal by a chelating agent on said treated and coated silica support obtained in step (d) to produce said silica-supported noble metal hydrogenation catalyst having a median pore size of at least 10 nm and no more than 300 nm.25. The method of claim 24 , wherein said noble metal is selected from the group consisting of ruthenium claim 24 , rhodium claim 24 , palladium claim 24 , platinum claim 24 , and mixtures thereof.26. The method of claim 25 , wherein said noble metal is ruthenium.27. The method of claim 24 , wherein said ...

CATALYTIC COMBUSTION IN LOW TEMPERATURE, HUMID CONDITIONS

Methods are disclosed for achieving the catalytic combustion of a gaseous species in low temperature humid environments. The methods comprise the steps of obtaining a combustion catalyst composition comprising an amount of a precious metal supported on an ion-exchangeable alkali metal titanate substrate, and then exposing the species to the combustion catalyst composition in the presence of an oxygen containing gas and water vapour at a catalysis temperature below 200° C. and at a relative humidity above 0.5%. A novel desiccant-coupled catalytic combustion process and system are also disclosed. 1. A method for the catalytic combustion of a gaseous species comprising:obtaining a combustion catalyst composition comprising an amount of a precious metal supported on an ion-exchangeable alkali metal titanate substrate; andexposing the species to the combustion catalyst composition in the presence of an oxygen containing gas and water vapour at a catalysis temperature below 200° C. and at a relative humidity above 0.5%,whereby the species is combusted with the oxygen at the combustion catalyst composition.2. The method of wherein the obtaining a combustion catalyst composition step comprises:obtaining an ion-exchangeable alkali metal titanate; andion exchanging the alkali metal titanate with the amount of the precious metal.3. The method of wherein the gaseous species is an unsaturated hydrocarbon claim 1 , an aldehyde claim 1 , or carbon monoxide.4. The method of wherein the gaseous species is ethylene claim 3 , formaldehyde claim 3 , or carbon monoxide.5. The method of wherein the gaseous species comprises ethylene.6. The method of comprising preparing the alkali metal titanate by the hydrothermal treatment of a mixture comprising an alkali metal hydroxide and a source of titania.7. The method of wherein the alkali metal titanate is sodium titanate.8. The method of wherein the alkali metal titanate has an ion exchange capacity greater than 2 meq/g.9. The method of ...

PLATINUM-CONTAINING CATALYSTS FOR COMBUSTION ENGINES

Emissions treatment systems of combustion engines are provided, which comprise a platinum-containing catalyst that is degreened during production, which is before exposure to operating conditions of a vehicle having a diesel engine. The platinum-containing catalyst, in the form of a platinum component on a high surface area refractory metal oxide support, exhibits a vibration frequency of about 2085 to about 2105 cmas measured by CO-DRIFTS. Such catalytic material is essentially-free of platinum oxide species found at greater than about 2110 cmas measured by CO-DRIFTS. Such catalysts can provide excellent and consistent conversion of nitrogen oxide (NO) to nitrogen dioxide (NO). 112-. (canceled)13. A method for forming a fully degreened diesel oxidation catalyst composite , the method comprising:obtaining a catalytic material comprising a platinum component on a high surface area refractory metal oxide support;depositing the catalytic material onto a carrier to form a diesel oxidation catalyst composite; andtreating the catalytic material at a temperature of at least about 500° C. in the presence of humidity and oxygen to form the fully degreened diesel oxidation catalyst composite.14. The method of claim 13 , wherein the catalytic material is provided as a slurry of the platinum component and the high surface area refractory metal oxide support.15. The method of claim 13 , wherein the treating step is conducted before the depositing step.16. The method of claim 13 , wherein the treating step is conducted after the depositing step.17. The method of claim 13 , wherein the high surface area refractory metal oxide support is first applied to the carrier claim 13 , followed by addition of the platinum component claim 13 , and wherein the catalytic material is treated after the step of depositing the platinum component onto the carrier.18. The method of claim 13 , wherein the temperature is in the range of about 550° C. to about 650° C.19. The method of claim 13 , ...

MOLECULAR SIEVE SSZ-116, ITS SYNTHESIS AND USE

A novel synthetic crystalline aluminogermanosilicate molecular sieve material, designated SSZ-116, is provided. SSZ-116 can be synthesized using 3-[(3,5-di-tert-butylphenyl)methyl]-1,2-dimethyl-1H-imidazolium cations as a structure directing agent. SSZ-116 may be used in organic compound conversion reactions and/or sorptive processes. 2. The molecular sieve of claim 1 , and having a composition comprising the molar relationship:{'br': None, 'sub': 2', '3', '2, 'i': 'n', 'AlO:()TO'}wherein n is ≥30; and T is a tetravalent element comprising silicon and germanium.3. The molecular sieve of claim 1 , and having a composition comprising the molar relationship:{'br': None, 'sub': 2', '3', '2, 'i': 'n', 'AlO:()TO'}wherein n is ≥50; and T is a tetravalent element comprising silicon and germanium.7. A method of synthesizing the molecular sieve of claim 4 , the method comprising: (1) a FAU framework type zeolite;', '(2) a source of germanium;', '(3) 3-[(3,5-di-tert-butylphenyl)methyl]-1,2-dimethyl-1H-imidazolium hydroxide (Q);', '(4) a source of fluoride ions; and', '(5) water; and, '(a) providing a reaction mixture comprising(b) subjecting the reaction mixture to crystallization conditions sufficient to form crystals of the molecular sieve.10. The method of claim 7 , wherein the FAU framework type is zeolite Y.11. The method of claim 7 , wherein the crystallization conditions include a temperature of from 125° C. to 200° C.12. The method of claim 7 , wherein the reaction mixture has a Q/F molar ratio in a range of 0.8 to 1.2.13. A process for converting a feedstock comprising an organic compound to a conversion product claim 1 , the process comprising contacting the feedstock at organic compound conversion conditions with a catalyst comprising the molecular sieve of . This disclosure relates to a novel synthetic crystalline molecular sieve designated SSZ-116, its synthesis, and its use in organic compound conversion reactions and sorption processes.Molecular sieves are a ...

PROCESS FOR PREPARING A CATALYST, CATALYST AND PROCESS FOR THE OXIDATIVE DEHYDROGENATION OF HYDROCARBONS

A process for preparing a catalyst provided in the form of a metal oxide catalyst having at least one element selected from Mo, Te, Nb, V, Cr, Dy, Ga, Sb, Ni, Co, Pt and Ce. The catalyst is subjected to an aftertreatment to increase the proportion of the M1 phase, by contacting the catalyst with steam at a pressure below 100 bar or by contacting the catalyst with oxygen to obtain an aftertreated catalyst. The aftertreated catalyst may be used for oxidative dehydrogenation processes. 1. A process for preparing a catalyst , wherein a catalyst is provided in the form of a metal oxide catalyst which comprises at least one element of the group Mo , Te , Nb , V , Cr , Dy , Ga , Sb , Ni , Co , Pt and Ce ,characterized in that is contacted with steam at a pressure below 100 bar, preferably below 80 bar, preferably below 50 bar, and/or', 'is contacted with oxygen., 'the catalyst is subjected to an aftertreatment to increase the fraction of the M1 phase of the catalyst, wherein the catalyst, with generation of an aftertreated catalyst,'}2. The process as claimed in claim 1 , characterized in that the catalyst claim 1 , during the aftertreatment claim 1 , is contacted with the steam and/or the oxygen at a temperature of at least 200° C. claim 1 , preferably at a temperature of at least 350° C. claim 1 , preferably at a temperature of at least 400° C. claim 1 , preferably at a temperature in the range from 200° C. to 650′ claim 1 , preferably at a temperature in the range from 300° C. to 650° C. claim 1 , preferably at a temperature in the range from 350° C. to 600° C. claim 1 , preferably at a temperature in the range from 350° C. to 550° C. claim 1 , preferably at a temperature in the range from 350° C. to 400° C. claim 1 , preferably at a temperature in the range from 400° C. to 500° C.3. The process as claimed in claim 1 , characterized in that the catalyst is a metal oxide catalyst comprising the elements Mo claim 1 , V claim 1 , Te claim 1 , Nb.4. The process as claimed ...

METHODS OF PRODUCING ORGANOSILICA MATERIALS AND USES THEREOF

Methods of preparing organosilica materials using a starting material mixture comprising at least one compound of Formula [(RO)SiCH](Ia) and at least one compound of Formula [R′ROSiCH](Ib), wherein each R′ independently represents an RO—, an R group, or an (RO)Si—CH— group, at least one R′ being (RO)Si—CH—; and R represents a C-Calkyl group, in the absence of a structure directing agent and/or porogen are provided herein. Processes of using the organosilica materials, e.g., for gas separation, etc., are also provided herein. 1. A method for preparing an organosilica material , the method comprising:{'sub': 2', '2', '3', '2', '3, '(a) providing a starting material mixture comprising at least one compound of Formula [(RO)SiCH](Ia) and at least one compound of Formula [R′ROSiCH](Ib), wherein'}{'sub': 3', '2', '3', '2, 'each R′ independently represents an RO— group, an R group, or an (RO)Si—CH— group, at least one R′ being (RO)Si—CH—; and'}{'sub': 1', '4, 'R represents a C-Calkyl group;'}(b) adding the starting material mixture into an acidic or basic aqueous mixture such that the resulting solution contains essentially no structure directing agent;(c) curing the solution to produce a pre-product; and{'sup': 1', '2', '1', '2, 'sub': 2', '3', '1', '4', '1', '4', '1', '4, '(d) drying the pre-product to obtain the organosilica material which is a polymer comprising independent siloxane units of Formula [RRSiCH](I), wherein each Rrepresents a hydroxyl group, a C-Calkoxy group, or an oxygen atom bonded to a silicon atom of another siloxane unit and each Rrepresents a hydroxyl group, a C-Calkoxy group, a C-Calkyl group, or an oxygen atom bonded to a silicon atom of another siloxane, wherein the organosilica material has an average pore diameter greater than about 1.0 nm.'}2. The method of claim 1 , wherein R represents a methyl or ethyl group claim 1 , preferably an ethyl group.3. The method of claim 1 , wherein the ratio between Formula (Ia) and Formula (Ib) is about 1:10 to ...

MESOPOROUS MIXED OXIDE CATALYST COMPRISING SILICON

A mesoporous mixed oxide catalyst that comprises silicon and at least one metal M that is selected from the group that consists of the elements of groups 4 and 5 of the periodic table and mixtures thereof, with the mass of metal M being between 0.1 and 20% of the mixed oxide mass. 1. Mesoporous mixed oxide catalyst that comprises silicon and at least one metal M that is selected from the group that consists of the elements of groups 4 and 5 of the periodic table and mixtures thereof , with the mass of metal M being between 0.1 and 20% of the mixed oxide mass , with said mixed oxide resulting from the combination of oxygen atoms with at least the silicon element and the element M.2. Catalyst according to claim 1 , in which said metal M is selected from the group that consists of tantalum claim 1 , niobium claim 1 , zirconium claim 1 , and mixtures thereof.3. Catalyst according to claim 1 , comprising a metal M′ claim 1 , with said metal M′ being a metal that is selected from the group that consists of the elements of groups 11 and 12 of the periodic table and mixtures thereof claim 1 , with the mass of metal M′ being between 0.1 and 20% of the mixed oxide mass.4. Catalyst according to claim 3 , in which said metal M′ is selected from the group that consists of silver claim 3 , copper claim 3 , zinc and mixtures thereof.5. Catalyst according to claim 1 , in which said mixed oxide is mesostructured.6. Catalyst according to claim 1 , in which the mixed oxide has a specific surface area of at least 250 m/g claim 1 , a pore volume of at least 1 ml/g and a mean pore diameter of at least 4 nm.7. Catalyst according to that is shaped in the form of balls claim 1 , pellets claim 1 , granules claim 1 , or extrudates claim 1 , or rings.8. Catalyst according to claim 7 , comprising at least one porous oxide material that has the role of binder claim 7 , with said porous oxide material being selected from the group that is formed by silica claim 7 , magnesia claim 7 , clays claim ...

CATALYST FOR PRODUCING HYDROGEN AND METHOD FOR PRODUCING HYDROGEN

A metal-supporting catalyst for decomposing ammonia into hydrogen and nitrogen. The catalyst shows a high performance with a low cost and being advantageous from the viewpoint of resources, and an efficient method for producing hydrogen using the catalyst. The catalyst catalytically decomposes ammonia gas to generate hydrogen. The hydrogen generation catalyst includes, as a support, a mayenite type compound having oxygen ions enclosed therein or a mayenite type compound having 10cmor more of conduction electrons or hydrogen anions enclosed therein, and metal grains for decomposing ammonia are supported on the surface of the support. Hydrogen is produced by continuously supplying 0.1-100 vol % of ammonia gas to a catalyst layer that comprises the aforesaid catalyst, and reacting the same at a reaction pressure of 0.01-1.0 MPa, at a reaction temperature of 300-800° C. and at a weight hourly space velocity (WHSV) of 500/mlghor higher. 1. A catalyst for producing hydrogen comprising a mayenite-type compound as a support which includes 10cmor more of conduction electrons or hydrogen anions , and metal particles for ammonia decomposition which are supported on a surface of the support.2. A catalyst for producing hydrogen comprising a mayenite-type compound as a support which includes oxygen ions which has not been made to include 10cmor more of conduction electrons or hydrogen anions , and metal particles for ammonia decomposition which are supported on a surface of the support.3. The catalyst for producing hydrogen according to claim 1 , wherein the catalytically active metal is at least one selected from the metal elements of Groups VIII claim 1 , IX claim 1 , and X.4. The catalyst for producing hydrogen according to claim 1 ,{'sup': 2', '−1, 'wherein the support includes a mayenite-type compound powder or compact and has an amount of the catalytically active metal particles of 0.01 wt % to 30 wt % and a BET specific surface area of 1 to 100 mg.'}5. A method for ...

TRANSITION-METAL-CONTAINING ZEOLITE

A transition-metal-containing silicoaluminophosphate zeolite having excellent high-temperature hydrothermal durability is easily and efficiently produced. A method for producing a transition-metal-containing zeolite that contains a silicon atom, a phosphorus atom, and an aluminum atom in at least its framework structure includes hydrothermal synthesis using an aqueous gel containing a silicon atom raw material, an aluminum atom raw material, a phosphorus atom raw material, a transition metal raw material, and a polyamine (other than diamines). A transition-metal-containing silicoaluminophosphate zeolite produced by hydrothermal synthesis using a zeolite raw material and the aqueous gel containing the transition metal raw material and the polyamine has excellent high-temperature hydrothermal durability and high catalytic activity. 1. An aluminophosphate zeolite containing 3% by weight or more transition metal M , wherein element mapping of the transition metal M in the zeolite determined with an electron probe microanalyzer shows that the coefficient of variation in intensity of the transition metal M is 33% or less and that the molar ratio of an aluminum atom to the total of a silicon atom and a phosphorus atom is 0.9 or more.2. The transition-metal-containing zeolite according to claim 1 , wherein the zeolite has an 8-membered ring structure in its framework structure3. The transition-metal-containing zeolite according to claim 1 , wherein the transition metal is iron and/or copper.4. The transition-metal-containing zeolite according to claim 1 , wherein the zeolite has a BET specific surface area of 500 m/g or more.5. The transition-metal-containing zeolite according to claim 1 , wherein the zeolite has a framework density of 10.0 T/1000 cubic angstroms or more and 16.0 T/1000 cubic angstroms or less in accordance with a zeolite structure defined by the International Zeolite Association (IZA).6. The transition-metal-containing zeolite according to claim 1 , ...

METAL TUNGSTATES FOR USE AS NITROGEN OXIDES REDUCTION CATALYSTS

A nitrogen oxide (NOx) reduction catalyst that includes a transition metal tungstate having the formula: MWOwherein M is selected from the group consisting of Mn, Fe, Co, Ni, and Cu. The catalyst may be utilized in various environments including oxygen rich and oxygen deficient environments. 1. A process of reducing nitrogen oxide (NOx) including the steps of:providing a gaseous exhaust mixture including nitrogen oxide (NOx) and hydrocarbon fuel;{'sub': '4', 'providing a nitrogen oxide (NOx) reduction catalyst including a transition metal tungstate having the formula: MWOwherein M is selected from the group consisting of Mn, Fe, Co, Ni, and Cu;'}contacting the gaseous exhaust mixture with a surface of the nitrogen oxide (NOx) reduction catalyst forming nitrogen, water and carbon dioxide.2. The process of wherein the gaseous exhaust mixture further includes oxygen.3. The process of wherein the nitrogen oxide (NOx) reduction catalyst includes a transition metal tungstate having the formula: MWOwherein M is selected from the group consisting of Mn claim 2 , Fe claim 2 , Co and Cu.4. The process of wherein the nitrogen oxide (NOx) reduction catalyst includes a transition metal tungstate having the formula: MWOwherein M is selected from the group consisting of Ni and Co and the catalyst reduces nitrogen oxide (NOx) in an oxygen deficient environment.5. The process of wherein the transition metal tungstate includes a crystalline structure.6. The nitrogen oxide (NOx) reduction catalyst of wherein the transition metal tungstate has a particle size of from 10 to 60 nanometers.7. The nitrogen oxide (NOx) reduction catalyst of wherein the catalyst has the formula: MnWOand the catalyst reduces nitrogen oxide (NOx) in the presence of oxygen.8. The nitrogen oxide (NOx) reduction catalyst of wherein the catalyst has significant selectivity to NOx conversion in the presence of oxygen such that the nitrogen oxide (NOx) conversion and oxygen conversion are approximately equal to one ...

Calcination Process to Produce Enhanced ODH Catalyst

Mixed metal oxide catalysts having an amorphous content of not less than 40 wt. % are prepared by calcining the catalyst precursor fully or partially enclosed by a porous material having a melting temperature greater than 600° C. in an inert container including heating the catalyst precursor at a rate from 0.5 to 10° C. per minute from room temperature to a temperature from 370° C. to 540° C. under a stream of pre heated gas chosen from steam and inert gas and mixtures thereof at a pressure of greater than or equal to 1 psig having a temperature from 300° C. to 540° C. and holding the catalyst precursor at that temperature for at least 2 hours and cooling the catalyst precursor to room temperature. 1. A method to calcine a catalyst precursor of the formula{'br': None, 'sub': 1', '0.1-1', '0.1-1', '0.01-0.2', '0.2', 'd, 'MoVNbTeXO'} calcining the catalyst precursor in an inert container with flow passage there through, at a rate from 0.5 to 10° C. per minute from room temperature to a holding temperature from 370° C. to 540° C. under a stream of pre heated gas chosen from steam and inert gas and mixtures thereof at a rate of flow comparable to a flow rate of not less 150 sccm through a 2.54 cm diameter tube, with a length of 152 cm at a pressure of greater than or equal to 1 psig having a temperature from 300° C. to 540° C.;', 'cooling the catalyst precursor to room temperature said catalyst precursor being fully or partially enclosed by a porous material having a melting temperature greater than 600° C.', 'holding the catalyst precursor at the holding temperature for at least 2 hours; and'}], 'where X is chosen from Pd, Sb Ba, Al, W, Ga, Bi, Sn, Cu, Ti, Fe, Co, Ni, Cr, Zr, Ca, oxides thereof and mixtures thereof, and d is a number to satisfy the valence of the catalyst while maintaining an amorphous content of not less than 40 wt. % the method comprising'}2. The method according to claim 1 , wherein the inert container is made from high temperature glass claim 1 , ...

CERIUM OXIDE PARTICLES AND METHOD FOR PRODUCTION THEREOF

The present invention relates to cerium oxide particles that have excellent heat resistance and/or pore volume especially useful for catalysts, functional ceramics, solid electrolyte for fuel cells, polishing, ultraviolet absorbers and the like, and particularly suitable for use as a catalyst or cocatalyst material, for instance in catalysis for purifying vehicle exhaust gas. The present invention also relates to a method for preparing such cerium oxide particles, and a catalyst, such as for purifying exhaust gas, utilizing these cerium oxide particles. 1. Cerium oxide particles having the following properties:{'sup': '2', 'a specific surface area (SBET) comprised between 45 and 80 m/g, after calcination at 900° C. for 5 hours, under air; and'}{'sup': '2', 'sub': 2', '2', '2, 'a specific surface area (SBET) comprised between 75 and 90 m/g after calcination at 700° C. for 4 hours, under a gaseous atmosphere containing 10% by volume of O, 10% by volume of HO and the balance of N.'}2. Cerium oxide particles according to having the following properties:{'sup': '2', 'a specific surface area (SBET) comprised between 55 and 80 m/g after calcination at 900° C. for 5 hours, under air; and'}{'sup': '2', 'sub': 2', '2', '2, 'a specific surface area (SBET) comprised between 75 and 90 m/g after calcination at 700° C. for 4 hours, under a gaseous atmosphere containing 10% by volume of O, 10% by volume of HO and the balance of N'}3. Cerium oxide particles according to claim 1 , further comprising at least one metal oxide claim 1 , other than cerium oxide claim 1 , the metal being selected from the group consisting of (1) metallic elements in Group 4A in the periodic table claim 1 , (2) metal elements in Group 4B in the periodic table claim 1 , such as titanium and zirconium claim 1 , (3) metal elements in Group 3A in the periodic table claim 1 , (4) alkali metal elements claim 1 , and (5) rare earth element (REE) or rare earth metal being selected from the fifteen lanthanides plus ...

PHOTOCATALYTIC REDUCTION OF CARBON DIOXIDE TO METHANOL OR CARBON MONOXIDE USING CUPROUS OXIDE

Provided herein are methods of COreduction to methanol or CO using a CuO catalyst. 1. A method of converting COto methanol comprising{'sub': 2', '2, 'irradiating CO, water, and CuO having a (i i 0) facet to form methanol, wherein i is 1 to 12.'}2. The method of claim 1 , wherein the irradiating comprises exposure to ultraviolet to visible light.3. The method of claim 1 , wherein the irradiating comprises exposure to light having one or more wavelengths from 200 to 650 nm.4. The method of claim 1 , wherein the water is present as a liquid.5. The method of claim 1 , wherein the water is present as water vapor.6. The method of claim 1 , wherein the (i i 0) facet is a (110) facet.7. The method of claim 6 , wherein the CuO having a (110) facet is octahedral claim 6 , truncated cubic claim 6 , or a mixture thereof.8. The method of claim 7 , wherein the irradiating comprises exposure to ultraviolet to visible light.9. The method of claim 8 , wherein the irradiating comprises exposure to light having one or more wavelengths from 200 to 650 nm.10. The method of claim 1 , where the method exhibits a quantum efficiency of at least 50%.11. The method of claim 10 , wherein the quantum efficiency is at least 70%.12. The method of claim 1 , wherein the COis continuously flowed through a suspension of the CuO in water during the irradiating.13. The method of claim 1 , wherein the CuO having a (i i 0) facet is prepared by a method comprising admixing copper acetate claim 1 , sodium hydroxide claim 1 , glucose claim 1 , and a surfactant and heating the admixture to 60° C. for 30-90 minutes to form the CuO having a (i i 0) facet.14. The method of claim 13 , wherein the surfactant comprises sodium dodecyl sulfate.15. A method of converting COto CO comprising{'sub': 2', '2', '2', '2, 'irradiating CO, water, and MoSadsorbed onto CuO to form CO, wherein the CuO has a (i i 0) facet, and i is 1 to 12.'}16. The method of claim 15 , wherein the irradiating comprises exposure to ultraviolet to ...

HIGHLY STABLE PLATINUM GROUP METAL (PGM) CATALYST SYSTEMS

A method of stabilizing a catalyst system includes hydrothermally treating an aluminum oxide catalyst support having ≥about 95 volume % of γ-AlOphase by heating to a temperature of about 800° C. to about 1,200° C. in the presence of water. A majority of the γ-AlOis converted to a stable alumina phase selected from the group consisting of: θ-AlO, δ-AlO, and combinations thereof to form a stabilized porous aluminum oxide support having an average surface area of ≥about 50 m/g to ≤about 150 m/g. A platinum group metal is then bound to a surface of the stable porous aluminum oxide support to form the stabilized catalyst systems. 1. A method of stabilizing a catalyst system comprising:{'sub': 2', '3, 'hydrothermally treating an aluminum oxide catalyst support comprising greater than or equal to about 95 volume % of γ-AlOphase by heating the support to a temperature of greater than or equal to about 700° C. to less than or equal to about 1,200° C. in air in the presence of water;'}{'sub': 2', '3', '2', '3', '2', '3, 'sup': 2', '2, 'converting a majority of the γ-AlOto a stable alumina phase selected from the group consisting of: θ-AlO, δ-AlO, and combinations thereof to form a stabilized porous aluminum oxide support having an average surface area of greater than or equal to about 50 m/g to less than or equal to about 150 m/g; and'}binding a platinum group metal to a surface of the stabilized porous aluminum oxide support to form the catalyst system.2. The method of claim 1 , wherein the temperature is greater than or equal to about 850° C. and less than or equal to about 1 claim 1 ,100° C.3. The method of claim 1 , further comprising calcining the catalyst system comprising the platinum group metal dispersed on the stabilized porous aluminum oxide support at a second temperature of greater than or equal to about 300° C. and less than or equal to about 650° C.4. The method of claim 1 , wherein the platinum group metal comprises a metal selected from the group consisting ...

METHOD FOR PRE-TREATING A CATALYST COMPOSITION

The present invention relates to a method for pre-treating a catalyst composition comprising contacting a medium pore aluminosilicate zeolite with an inert gas comprising water vapour or alcohol vapour at a temperature between 30° C. and the boiling temperature of water or the alcohol. 1. A method for pre-treating a catalyst composition comprising: contacting a medium pore aluminosilicate zeolite with an inert gas comprising water vapour or alcohol vapour at a temperature between 30° C. and the boiling temperature of water or the alcohol to form the pre-treated catalyst.2. The method according to claim 1 , wherein the alcohol is at least one selected from 1-propanol claim 1 , isopropanol claim 1 , isobutanol claim 1 , tertiary butanol claim 1 , and a mixture thereof.3. The method according to claim 2 , wherein the inert gas is at least one selected from nitrogen claim 2 , helium claim 2 , argon claim 2 , and a mixture thereof.4. The method according to claim 3 , wherein the zeolite is a 10-ring zeolite having pores formed by a ring consisting of 10 SiOtetrahedra.5. The method according to claim 4 , wherein the zeolite has a pore size of 5-6 Å.6. The method according to claim 5 , wherein the zeolite is of the ZSM-5 type.7. The method according to claim 6 , wherein the silicon to aluminium (Si:Al) molar ratio of the zeolite is 10-100.8. The method according to claim 7 , wherein the zeolite comprises up to 1 wt-% of at least one element selected from Groups 6 and 9 of the Periodic Table.9. The method according to claim 8 , wherein the element is at least one selected from molybdenum claim 8 , tungsten claim 8 , cobalt claim 8 , and rhodium.10. The method according to claim 9 , wherein the amount of the water vapour or the alcohol vapour in the inert gas is at least 50 wt % of the saturation level of the water vapour or the alcohol vapour in the inert gas.11. A pre-treated catalyst composition obtainable by the method according to .12. Process for the dimerization of ...

PROCESS FOR THE CATALYTIC REMOVAL OF CARBON DIOXIDE, NOx FROM EXHAUST GASES

The present invention relates to a method for the catalytic removal of carbon dioxide and NO x from waste gases in a reactor charged with activated carbon catalyst. The method comprises the following steps: a. saturating the catalyst with water b. saturating or partially saturating the waste gases with water, c. introducing the waste gases into the reactor, d. catalytically converting NOx into NO 2 − and, in parallel with this, catalytically converting CO 2 into carbon and O 2 on the same catalyst, e. washing out the activated carbon catalyst with water and discharging the carbon as a solid and NO 2 — dissolved in water or in the base.

TOLUENE DISPROPORTIONATION USING AN ENHANCED UZM-39 ALUMINOSILICATE ZEOLITE

Toluene disproportionation processes utilizing treated UZM-39 zeolites are described. The processes produce effluent streams comprising para-xylene and benzene. The molar ratio of benzene to xylene (Bz/X) in the effluent stream can be in a range of about 1.00 to about 1.14, the molar ratio of para-xylene to xylene (pX/X) in the effluent stream can be in a range of about 0.80 to about 1.0, and the conversion of toluene can be about 20% to about 40%. 1. A toluene disproportionation process comprising contacting a feed comprising toluene with a catalyst comprising a microporous crystalline zeolite at disproportionation conditions to produce an effluent stream comprising para-xylene and benzene , wherein a molar ratio of benzene to xylene in the effluent stream is in a range of about 1.00 to about 1.14 , wherein a molar ratio of para-xylene to xylene in the effluent stream is in a range of about 0.80 to about 1.0 , and wherein a conversion of toluene is about 20% to about 40%; andwherein the zeolite has been enhanced with at least one enhancement selected from treatment for deposition of carbon, treatment for deposition of silica, or both.2. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08.4. (canceled)5. The process of wherein the at least one enhancement treatment step comprises at least one treatment to incorporate silica.6. The process of wherein the catalyst is steamed after the at least one enhancement treatment step.7. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08 and wherein the range of the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.95.8. The process of wherein a selectivity to xylenes is greater than 52% when the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.90.9. The process of wherein a selectivity to light ends is less than about 3.5% when the molar ratio of para-xylene to xylene ...

TOLUENE DISPROPORTIONATION USING AN ENHANCED UZM-44 ALUMINOSILICATE ZEOLITE

Toluene disproportionation processes utilizing treated UZM-44 zeolites are described. The processes produce effluent streams comprising para-xylene and benzene. The molar ratio of benzene to xylene (Bz/X) in the effluent stream can be in a range of about 1.00 to about 1.14, the molar ratio of para-xylene to xylene (pX/X) in the effluent stream can be in a range of about 0.80 to about 1.0, and the conversion of toluene can be about 20% to about 40%. 1. A toluene disproportionation process comprising contacting a feed comprising toluene with a catalyst comprising a microporous crystalline zeolite at disproportionation conditions to produce an effluent stream comprising para-xylene and benzene , wherein the zeolite is UZM-44 , wherein a molar ratio of benzene to xylene in the effluent stream is in a range of about 1.00 to about 1.14 , wherein a molar ratio of para-xylene to xylene in the effluent stream is in a range of about 0.80 to about 1.0 , wherein a conversion of toluene is about 20% to about 40%; andwherein the catalyst has been enhanced with at least one enhancement treatment step selected from treatment for deposition of carbon, treatment for deposition of silica, or both.2. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08.4. (canceled)5. The process of wherein the at least one enhancement treatment step comprises at least one treatment to incorporate silica.6. The process of wherein the catalyst is steamed after the at least one enhancement treatment step.7. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08 and wherein the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.95.8. The process of wherein a selectivity to xylenes is greater than 52% when the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.90.9. The process of wherein a selectivity to light ends is less than about 3.5% when the molar ...

METHOD FOR SYNTHESIZING SILVER NANOPARTICLES ON TiO2 USING HYBRID POLYMERS

Hybrid TiO 2 nanostructures with engineered morphologies (flakes, spheres and buds) supporting Ag nanocrystals were synthesized based on cooperative sol-gel chemistry of either titanium iso-propoxide or N-butoxide and assembled with polyvinyl alcohol and polyethylene glycol.

PROCESSES USING MOLECULAR SIEVE SSZ-102

Uses are disclosed for a new crystalline molecular sieve designated SSZ-102 synthesized using an N,N′-dimethyl-1,4-diazabicyclo[2.2.2]octane dication as a structure directing agent. SSZ-102 has ESV framework topology. 1. A process for treating a cold-start engine exhaust gas stream containing hydrocarbons and other pollutants consisting of flowing the engine exhaust gas stream over a molecular sieve bed which preferentially adsorbs the hydrocarbons over water to provide a first exhaust stream , and flowing the first exhaust gas stream over a catalyst to convert any residual hydrocarbons and other pollutants contained in the first exhaust gas stream to innocuous products and provide a treated exhaust stream and discharging the treated exhaust stream into the atmosphere , the molecular sieve bed comprising a molecular sieve having ESV framework topology and having a mole ratio of from 5 to 12.2. The process of claim 1 , wherein the molecular sieve has a SiO/AlOmole ratio of from 5 to 10.3. The process of claim 1 , wherein the engine is an internal combustion engine.4. The process of claim 3 , wherein the internal combustion engine is an automobile engine.5. The process of claim 1 , wherein the engine is fueled by a hydrocarbon fuel.6. The process of claim 1 , wherein the molecular sieve has deposited on it a metal selected from the group consisting of ruthenium claim 1 , rhodium claim 1 , palladium claim 1 , platinum claim 1 , and mixtures thereof.7. The process of claim 6 , wherein the metal is selected from the group consisting of palladium claim 6 , platinum claim 6 , and mixtures thereof. This application is a divisional application of co-pending U.S. patent application Ser. No. 14/716,784, filed on May 19, 2015, which claims the benefit of U.S. Provisional Patent Application Ser. No. 62/068,541, filed on Oct. 24, 2014, the disclosures of which are incorporated herein by reference in their entirety.This disclosure is directed to a new crystalline molecular sieve ...

ALUMINUM GRADIENT ALUMINOSILICATE ZEOLITE COMPOSITIONS

Disclosed herein are compositions comprising an aluminosilicate zeolite crystals with an 8 ring pore size having a depth dependent silica to alumina molar ratio and processes of making aluminosilicate zeolite crystals with an 8 ring pore size having a depth dependent silica to alumina molar ratio. 1. A composition comprising:an aluminosilicate zeolite crystal with an 8 ring pore size, the aluminosilicate zeolite crystal having a surface silica to alumina molar ratio and an internal silica to alumina molar ratio, wherein the surface silica to alumina molar ratio is either higher or lower than the internal silica to alumina molar ratio.2. The composition of claim 1 , wherein the aluminosilicate zeolite crystal comprises structural codes selected from the group consisting of AEI claim 1 , AFX claim 1 , CHA claim 1 , LEV claim 1 , AFT claim 1 , EAB claim 1 , KFI claim 1 , SAT claim 1 , TSC claim 1 , SAV claim 1 , ERI claim 1 , and combinations thereof.3. The composition of claim 1 , wherein the aluminosilicate zeolite crystal comprises CHA.4. The composition of claim 1 , wherein the composition is about 80% or more crystalline on a molar basis.5. The composition of claim 4 , wherein the composition is about 80% to about 95% crystalline on a molar basis.6. The composition of claim 1 , wherein the composition has a zeolitic BET surface area of about 400 m/g or more.7. The composition of claim 1 , wherein the surface silica to alumina molar ratio is one or more of the following:at least about 50 times higher or lower than the maximum value of the internal silica to alumina molar ratio;at least about 30 times higher or lower than the maximum value of the internal silica to alumina molar ratio;at least about 10 times higher or lower than the maximum value of the internal silica to alumina molar ratio;at least about 5 times higher or lower than the maximum value of the internal silica to alumina molar ratio; orat least about 1.5 times higher or lower than the maximum value of ...

Catalyst for thermochemical water splitting

The present invention relates to a catalyst for the thermochemical generation of hydrogen from water and/or the thermochemical generation of carbon monoxide from carbon dioxide comprising a solid solution of cerium dioxide and uranium dioxide.

PROCESS FOR SYNTHESIZING A METAL-DOPED ALUMINOGALLATE NANOCOMPOSITE AND METHODS OF USE THEREOF

The present disclosure relates to a process for producing a finely divided metal-doped aluminogallate nanocomposite comprising mixing a carrier solvent with a bulk metal-doped aluminogallate nanocomposite to form a bulk metal-doped aluminogallate slurry and atomizing the bulk metal-doped aluminogallate slurry using a low temperature collision to produce a finely divided metal-doped aluminogallate nanocomposite, the composition of a nickel-doped aluminogallate nanocomposite (GAN), and a method of NO decomposition using the nickel-doped aluminogallate nanocomposite. 1: A process for producing a finely divided metal-doped aluminogallate nanocomposite comprising: [{'sub': 2', '3, 'GaO;'}, {'sub': 2', '3, 'AlO; and'}, 'at least one metal oxide dopant comprising a metal selected from the group consisting of Cr, Mn, Fe, Co, Ni, Cu, Zn, Ag, Au, Pd, Pt, Ru, Rh, In, Ir, Tl, Ge, and Sn; and, 'mixing a carrier solvent with a bulk metal-doped aluminogallate nanocomposite synthesized by a process selected from the group consisting of co-precipitation, sol-gel, and hydrothermal to form a bulk metal-doped aluminogallate slurry, wherein the bulk metal-doped aluminogallate nanocomposite comprisesatomizing the bulk metal-doped aluminogallate slurry using a collision to produce the finely divided metal-doped aluminogallate nanocomposite;wherein the carrier solvent is at least one selected from the group consisting of deionized water, ethanol, butanol, isopropyl alcohol, diacetone alcohol, diglycol, triglycol, acetone, methyl ethyl ketone, ethyl acetate, butyl acetate, toluene, and xylene.2: The process of claim 1 , wherein the bulk metal-doped aluminogallate is synthesized by a hydrothermal process comprising:adding a precipitating agent to an aqueous solution comprising a gallium salt, an aluminum salt, and a metal dopant salt to form a metal-doped aluminogallate suspension with a pH of 8-12; andheating the metal-doped aluminogallate suspension to a hydrothermal reaction temperature ...

Molding for a hydrophobic zeolitic material and process for its production

The present invention relates to A process for the production of a molding, comprising (I) providing a zeolitic material; (II) mixing the zeolitic material provided in step (I) with one or more binders; (III) kneading of the mixture obtained in step (II); (IV) molding of the kneaded mixture obtained in step (III) to obtain one or more moldings; (V) drying of the one or more moldings obtained in step (IV); and (VI) calcining of the dried molding obtained in step (V); wherein the zeolitic material provided in step (I) displays a water adsorption ranging from 1 to 15 wt.-% when exposed to a relative humidity of 85%, as well as to a molding obtainable or obtained according to the inventive process in addition to a molding per se and to their respective use.

METHOD FOR PREPARING BI-COMPONENT, MULTI-NETWORK NANOFIBROUS AEROGEL-SUPPORTED HETEROJUNCTION PHOTOCATALYST AND APPLICATION THEREOF

A method for preparing a bi-component, multi-network nanofibrous aerogel-supported heterojunction photocatalyst includes the following steps. Step 1, preparing ammoniated polyacrylonitrile nanofibers. Step 2, dispersing the ammoniated polyacrylonitrile nanofibers in water to obtain a first solution; dispersing cellulose nanofibers in water to obtain a second solution; and mixing, heating and lyophilizing the first solution with the second solution to obtain a bi-component, multi-network nanofibrous aerogel. Step 3, adding graphite carbon nitride, a ferric-iron containing reagent, 2,5-diaminoterephthalic acid, and the bi-component, multi-network nanofiber aerogel obtained in the step 2 into a N, N-dimethylformamide solvent to obtain a third solution, and carrying out a hydrothermal reaction on the third solution for 8-24 hours to obtain the bi-component, multi-network nanofibrous aerogel-supported heterojunction photocatalyst. 1. A method for preparing a bi-component , multi-network nanofibrous aerogel-supported heterojunction photocatalyst , comprising the following steps:step 1, preparing ammoniated polyacrylonitrile nanofibers;step 2, dispersing the ammoniated polyacrylonitrile nanofibers in water to obtain a first solution; dispersing cellulose nanofibers in water to obtain a second solution; and mixing, heating and lyophilizing the first solution with the second solution to obtain a bi-component, multi-network nanofibrous aerogel; andstep 3, adding graphite carbon nitride, a ferric-iron containing reagent, 2,5-diaminoterephthalic acid, and the bi-component, multi-network nanofiber aerogel obtained in the step 2 into a N, N-dimethylformamide solvent to obtain a third solution, and carrying out a hydrothermal reaction on the third solution for 8-24 hours to obtain the bi-component, multi-network nanofibrous aerogel-supported heterojunction photocatalyst.2. The method according to claim 1 , wherein claim 1 , the step of preparing the ammoniated polymer nanofibers ...

GERMANOSILICATE COMPOSITIONS AND METHODS OF PREPARING THE SAME

The present disclosure is directed to novel germanosilicate compositions and methods of producing the same. In particular, this disclosure describes an array of transformations originating from the extra-large-pore crystalline germanosilicate compositions, designated CIT-13, possessing 10- and 14-membered rings. Included among the new materials are the new phyllosilicate compositions, designated CIT-13P, new crystalline microporous germanosilicates including high silica versions of CIT-5 and CIT-13, with and without added metal oxides, and new germanosilicate compounds designated CIT-14 and CIT-15. The disclosure also describes methods of preparing these new germanosilicate compositions as well as the compositions themselves. 1. A silicate crystalline composition derived from at least one transformation of a crystalline microporous , optionally hydrothermally derived , CIT-13 germanosilicate.2. The crystalline silicate composition of claim 1 , further comprising at least one oxide of a metal or metalloid claim 1 , M claim 1 , where M is aluminum claim 1 , boron claim 1 , gallium claim 1 , germanium claim 1 , hafnium claim 1 , iron claim 1 , tin claim 1 , titanium claim 1 , vanadium claim 1 , zinc claim 1 , or zirconium.3. The crystalline silicate composition of claim 1 , that is microporous and the result of degermanating the crystalline microporous claim 1 , optionally hydrothermally derived claim 1 , CIT-13 germanosilicate.4. The crystalline silicate composition of claim 1 , that is microporous claim 1 , having a Si/Ge ratio in a range of from about 25 to about 250.5. The crystalline silicate composition of further comprising at least one oxide of a metal or metalloid claim 4 , M claim 4 , where M is aluminum claim 4 , boron claim 4 , gallium claim 4 , hafnium claim 4 , iron claim 4 , silicon claim 4 , tin claim 4 , titanium claim 4 , vanadium claim 4 , zinc claim 4 , or zirconium claim 4 , in a Si/M ratio in a range from about 25 to about 250.6. The crystalline ...