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 ПРЕВРАЩЕНИЯ ОЛЕФИНА ИЛИ СПИРТА И СПОСОБ ПОЛУЧЕНИЯ ПРОПИЛЕНА ИЛИ АРОМАТИЧЕСКОГО СОЕДИНЕНИЯ

Изобретение относится к способу превращения олефина или спирта и способу получения пропилена или ароматического соединения. Способ превращения олефина или спирта включает этап предварительной обработки, в котором получают проводящий катализатор путем загрузки реактора с псевдоожиженным слоем непроводящим катализатором, содержащим цеолит и/или оксид кремния, и подачи нагретого углеводородного газа в реактор с псевдоожиженным слоем для осаждения углеродистого кокса и нанесения на непроводящий катализатор, и этап превращения олефина или спирта с помощью реакции в псевдоожиженном слое, в котором используют данный проводящий катализатор, где скорость подачи газа составляет 0,40 м/с или менее на стадии предварительной обработки в виде скорости потока газа в реакторе с псевдоожиженным слоем, и скорость подачи газа составляет 0,5 м/с или более на стадии превращения олефина или спирта в виде скорости потока газа в реакторе с псевдоожиженным слоем. Изобретение обеспечивает подавление электростатического ...

СПОСОБ ПРИГОТОВЛЕНИЯ КАТАЛИЗАТОРА ГИДРОКРЕКИНГА

Изобретение относится к способу приготовления сульфидированного катализатора гидрокрекинга, содержащему этапы, где (a) пропитывают аморфный алюмосиликатный носитель раствором, содержащим компоненты с одним или более металлами VIB группы, компоненты с одним или более металлами VIII группы и С-Смногоатомное соединение, посредством одноступенчатой пропитки, (b) сушат обработанный носитель катализатора при температуре самое большее 200°С с образованием пропитанного носителя, и (c) сульфидируют пропитанный носитель с получением сульфидированного катализатора, причем С-Смногоатомное соединение представляет собой сахар, сахарный спирт и/или сахарную кислоту, и причем способ осуществляют в отсутствие промежуточного прокаливания. Изобретение также относится к способу гидрокрекинга углеводородного потока. Технический результат заключается в получении более стабильного катализатора, демонстрирующего увеличенную активность гидрокрекинга. 2 н. и 7 з.п. ф-лы, 3 табл., 6 пр.

ЦЕОЛИТЫ, СОДЕРЖАЩИЕ ФОСФОР/СЕРУ-ПЕРЕХОДНЫЙ МЕТАЛЛ, ДЛЯ РАЗЛОЖЕНИЯ NO

Настоящее изобретение касается применения цеолитового катализатора для снижения содержания оксидов азота в газе, а также способа снижения содержания оксидов азота в газе при помощи приведения этого газа в контакт с указанным цеолитовым катализатором. Для уменьшения содержания оксидов азота в газе применяют цеолитовый катализатор, который содержит по меньшей мере железо и дополнительно атомы серы, причем атомы серы присутствуют в концентрации от 0,2 до 3% масс. в пересчете на весь катализатор и цеолит выбран из группы, состоящей из BEA, FAU, FER, MFI и их смесей. Технический результат - катализатор при более низкой температуре реакции проявляет достаточно высокую активность. 2 н. и 7 з.п. ф-лы, 2 табл.

СПОСОБ ПОЛУЧЕНИЯ МЕТАЛЛООБМЕННЫХ ЦЕОЛИТОВ ПОСРЕДСТВОМ ИОННОГО ОБМЕНА В ТВЁРДОМ СОСТОЯНИИ ПРИ НИЗКИХ ТЕМПЕРАТУРАХ

Настоящее изобретение относится к способу получения металлообменных цеолитных материалов посредством воздействия на физическую смесь оксида металла и цеолитного материала, имеющего ионообменную способность, атмосферой, содержащей аммиак, при температуре 150-250°С, а также к способам для каталитического восстановления NO, например, в выхлопах электрических станций или в выхлопах дизельных двигателей, в присутствии полученного цеолитного материала. Способ получения металлообменного цеолитного материала или смесей металлообменных цеолитных материалов включает следующие стадии: предоставление сухой смеси, содержащей а) один или более цеолитных исходных материалов, которые имеют каркасную структуру с обозначением MFI и которые проявляют ионообменную способность, и b) одно или более соединений металлов; нагревание смеси в газообразной атмосфере, содержащей аммиак, при температуре между 150°С и 250°С и в течение времени, достаточного для инициации и осуществления ионного обмена в твердом состоянии ...

СПОСОБ ПОЛУЧЕНИЯ ЛЕГКИХ ОЛЕФИНОВ

Изобретение относится к способу получения легких олефинов, где в способе получения легких олефинов путем непрерывного контактирования сырья на основе кислородсодержащих соединений и катализатора для осуществления реакции дегидратации реакционное давление Р реакции дегидратации находится в диапазоне 1,2-2,8 МПа, среднечасовая скорость подачи сырья Н в реакцию дегидратации находится в диапазоне 7-250 час, где в ходе реакции дегидратации Н и Р удовлетворяют математической функции H=f(P), которая является строго возрастающей функцией. Способ получения легких олефинов реализуется в простом и непрерывном производственном процессе, приводит к значительному увеличению производства легких олефинов и характеризуется высокой безопасностью. 14 з.п. ф-лы, 3 пр., 6 табл., 7 ил.

АЛЮМОСИЛИКАТНЫЙ ЦЕОЛИТ, СОДЕРЖАЩИЙ ПЕРЕХОДНЫЙ МЕТАЛЛ

Изобретение относится к каталитической системе очистки выхлопных газов. Предложен синтетический алюмосиликатный цеолитный катализатор, содержащий медь в качестве каталитически активного компонента. Катализатор содержит алюмосиликатный цеолит типа шабазит. Максимальный размер кольца цеолита составляет восемь тетраэдрических атомов. Средний размер кристаллитов цеолита, определенный сканирующей электронной микроскопией, составляет более 0,50 микрометра. Изобретение обеспечивает повышенную селективность восстановления оксидов азота в выхлопных газах двигателей внутреннего сгорания. 3 н. и 14 з.п. ф-лы, 2 табл., 4 пр.

КАТАЛИЗАТОР ДЛЯ ПРОИЗВОДСТВА АРОМАТИЧЕСКИХ УГЛЕВОДОРОДНЫХ СОЕДИНЕНИЙ

Изобретение относится к способу получения ароматических углеводородных соединений из легких углеводородов посредством каталитической реакции циклизации и к катализатору для ее использования. Представлен цеолитсодержащий прессованный катализатор для использования в способе производства ароматических углеводородных соединений методом каталитической циклизации из легкоуглеводородного сырья, в котором цеолит, содержащийся в цеолитсодержащем прессованном катализаторе, удовлетворяет следующим условиям: (а) цеолит является цеолитом со средним диаметром пор от 5 до 6,5 Å; (б) цеолит имеет диаметр первичной частицы в ряду от 0,02 до 0,25 мкм; и (в) цеолит содержит, по крайней мере, один металлический элемент, выбранный из группы, состоящей из металлов, принадлежащих к IB группе периодической системы, в виде соответствующих катионов, и где цеолитсодержащий прессованный катализатор включает в себя, по меньшей мере, один элемент, выбранный из группы, состоящей из элементов, принадлежащих к IB, IIB, ...

КАТАЛИЗАТОРЫ СКВ: ПЕРЕХОДНЫЙ МЕТАЛЛ/ЦЕОЛИТ

Изобретение относится к способу превращения оксидов азота в азот. Способ осуществляется путем контактирования оксидов азота с азотистым восстанавливающим агентом в присутствии синтетического цеолитного катализатора, содержащего от 0,1 до 10 мас.% металла, в расчете на общую массу цеолитного катализатора. При этом металл выбирают из Cu, Fe или их комбинации. Цеолитный катализатор нанесен на подложку фильтра и представляет собой силикоалюмофосфатный цеолит (SAPO), имеющий структуру СНА. Изобретение позволяет создать эффективные СКВ-катализаторы, которые имеют хорошую низкотемпературную СКВ-активность, высокую селективность к N, и хорошую термическую стойкость, а также являются относительно устойчивыми к ингибированию углеводородами. 3 н. и 14 з.п. ф-лы, 2 табл., 23 ил.

КАТАЛИТИЧЕСКИЕ КОМПОЗИЦИИ ФКК, СОДЕРЖАЩИЕ ОКСИД БОРА

Описаны композиции крекинга с флюидизированным катализатором (ФКК), способы производства и их применение. Каталитическая композиция крекинга с флюидизированным катализатором (ФКК) для крекинга углеводородов включает нецеолитный матричный компонент, оксид бора, пропитывающий матрицу, и крекирующие частицы, где нецеолитный матричный компонент включает алюмосиликат и крекирующие частицы включают цеолит и нецеолитный компонент. Каталитическая композиция ФКК способствует уменьшению выработки кокса и водорода во время крекинга металлсодержащего сырья ФКК, по сравнению с каталитической композицией ФКК без оксида бора, пропитывающего нецеолитную матрицу и крекирующие частицы, которые включают цеолит и нецеолитный компонент. Оксид бора пассивирует сырье ФКК, имеющее высокое содержание металлов во время ФКК. Каталитические композиции ФКК могут быть применены для крегинга углеводородного сырья, особенно сырья остатков вакуумной перегонки, содержащего высокие уровни V и Ni, что приводит к меньшим выходам ...

ПОКРЫТИЕ ДЛЯ ВОССТАНОВЛЕНИЯ ОКСИДОВ АЗОТА

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

КАТАЛИЗАТОР И СПОСОБ АРОМАТИЗАЦИИ С-СГАЗОВ, ЛЕГКИХ УГЛЕВОДОРОДНЫХ ФРАКЦИЙ АЛИФАТИЧЕСКИХ СПИРТОВ, А ТАКЖЕ ИХ СМЕСЕЙ

Изобретение относится к технологии переработки углеводородного сырья, в частности к катализаторам и технологии ароматизации углеводородных газов С-С, легких низкооктановых углеводородных фракций и кислородсодержащих соединений, а также их смесей с получением концентрата ароматических углеводородов. Катализатор содержит механическую смесь двух цеолитов. Первый цеолит охарактеризован силикатным модулем SiO/AlO=20. Цеолит предварительно обработан водным раствором щелочи и модифицирован оксидами редкоземельных элементов в количестве от 0,5 до 2,0 мас.% от массы первого цеолита. Второй цеолит охарактеризован силикатным модулем SiO/AlO=82. Цеолит содержит остаточные количества оксида натрия 0,04 мас.% от массы второго цеолита и модифицирован оксидом магния в количестве от 0,5 до 5,0 мас.% от массы второго цеолита. Цеолиты использованы в массовом соотношении от 1,7/1 до 2,8/1. Связующее содержит, по меньшей мере, оксид кремния и использовано в количестве от 20 до 25 мас.% от массы катализатора ...

АЛЮМОСИЛИКАТНЫЙ ЦЕОЛИТ, СОДЕРЖАЩИЙ ПЕРЕХОДНЫЙ МЕТАЛЛ

... 1. Синтетический алюмосиликатный цеолитный катализатор, содержащий, по меньшей мере, один каталитически активный переходный металл, выбранный из группы, состоящей из Cu, Fe, Hf, La, Au, In, V, лантаноидов и переходных металлов VIII группы, который представляет собой алюмосиликатный цеолит с небольшими порами, имеющий максимальный размером кольца, составляющий восемь тетраэдрических атомов, причем средний размер кристаллитов алюмосиликатного цеолита, определенный сканирующей электронной микроскопией, составляет >0,50 мкм.2. Алюмосиликатный цеолитный катализатор по п.1, в котором, по меньшей мере, один каталитически активный переходный металл представляет собой медь, железо или медь и железо.3. Алюмосиликатный цеолитный катализатор по п.1 или 2, в котором, по меньшей мере, один каталитически активный переходный металл является медью.4. Алюмосиликатный цеолитный катализатор по п.1, в котором средний размер кристаллитов составляет >1,00 мкм.5. Алюмосиликатный цеолитный катализатор по п.1, в ...

КАТАЛИТИЧЕСКАЯ СИСТЕМА И СПОСОБ ГИДРОПЕРЕРАБОТКИ ТЯЖЕЛЫХ МАСЕЛ

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

СПОСОБ ПОЛУЧЕНИЯ МЕТАЛЛООБМЕННЫХ ЦЕОЛИТОВ ПОСРЕДСТВОМ ИОННОГО ОБМЕНА В ТВЁРДОМ СОСТОЯНИИ ПРИ НИЗКИХ ТЕМПЕРАТУРАХ

КАТАЛИЗАТОР ДЛЯ ПИРОЛИЗА СЫРЬЯ

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КАТАЛИТИЧЕСКИЕ СИСТЕМЫ ДЛЯ СЕЛЕКТИВНОГО КАТАЛИТИЧЕСКОГО ВОССТАНОВЛЕНИЯ

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

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

АДСОРБИРУЮЩЕЕ ВЕЩЕСТВО ДЛЯ ДЕСУЛЬФУРИЗАЦИИ УГЛЕВОДОРОДНОГО МАСЛА, ЕГО ПОЛУЧЕНИЕ И ПРИМЕНЕНИЕ

... 1. Адсорбирующее вещество для десульфуризации углеводородного масла, содержащее следующие компоненты в расчете на общую массу адсорбирующего вещества:1) Si-Al молекулярное сито со структурой BEA в количестве 1-20% масс.,2) по меньшей мере одно связующее, выбранное из группы, состоящей из диоксида титана, диоксида олова, диоксида циркония и оксида алюминия, в количестве 3-35% масс.,3) источник диоксида кремния в количестве 5-40% масс.,4) оксид цинка в количестве 10-80% масс., и5) по меньшей мере один металл-промотор, выбранный из группы, состоящей из кобальта, никеля, железа и марганца, в зависимости от металла в количестве 5-30% масс., где по меньшей мере 10% масс. металла-промотора присутствует в состоянии пониженной валентности.2. Адсорбирующее вещество по п. 1, в котором Si-Al молекулярное сито со структурой BEA присутствует в количестве 2-15% масс., связующее присутствует в количестве 5-25% масс., источник диоксида кремния присутствует в количестве 10-30% масс., оксид цинка присутствует ...

Катализатор для очистки выхлопных газов от окислов азота

Verfahren zur Entfernung von Stickstoffoxiden aus Abgasen

Verwendung eines Katalysators zur Verringerung der Partikelmenge und/oder -größe im Dieselabgas

PRODUCTION OF AROMATICS FROM ETHANE AND/OR ETHYLENE

Selective hydrogenation of olefins in naphthas - using three-component catalyst and single stage operation

Process and three-component catalyst system for selective hydrogenation of olefins in hydrocarbon mixts. contg. aromatics comprising (a) an inorganic non-crystalline support component, (b) 10-70 (10-30)% wt. crystalline aluminosilicate component with silica to alumina mole ratio >=2.5 and alkali metal content 2.0% wt. (as oxide), and (c) 1-25% wt (based on (a) component) transition metal hydrogenation component (Group VIB or VIII metal and/or oxide and/or sulphide, pref. chosen from Ni, Mo and/or W). Pref. component (a) is alumina, or silica-stabilised alumina or magnesia, where pref. silica to alumina (or magnesia) ratio is 1:4-6. Process operating conditions are 150-700 degrees F, (pref. inlet 200-280 degrees F, outlet 450-650 degrees F) 100-1000 (400) psign. H2 feed rate > 500 (>1000) SCF/B, and contact time 0.25-8 hrs (pref. 1-2). Catalyst and processis esp. suitable for hydrogenation of olefins in gasoline range materials.

Verfahren zur Herstellung eines formselektiven kristallinen Aluminiumsilikat-Katalysators mit Hydrierungs-Dehydrierungs-Aktivitaet und Anwendung des Katalysators zur Umsetzung eines organischen Beschickungsmaterials

IMPROVEMENTS RELATING TO CATALYSTS AND THE USE THEREOF

... 1,248,435. Hydrocracking catalysts. TEXACO DEVELOPMENT CORP. 22 Oct., 1968 [27 Oct., 1967], No. 49950/68. Heading B1E. [Also in Division C5] A hydrocracking catalyst comprises (1) a hydrogenating component which comprises at least one metal selected from Group VI and Group VIII and (2) a cracking component which consists essentially of a mixture of (a) amorphous inorganic oxide material selected from silica, alumina, zirconia, magnesia and mixtures thereof and (b) crystalline zeolite having an alkali metal content (calculated as the oxide) of not greater than 1.0 weight per cent, the zeolite constituting from 5 to 55 weight per cent of the cracking component and the rare earth metal content of the cracking component being less than 0.1 weight per cent. The metal selected from Group VI and Group VIII may be chromium, molybdenum, tungsten, cobalt, nickel or a metal of the palladium and platinum triads, for example palladium, and may be in the form of elemental metal, oxide, sulphide or a ...

Catalytic conversion of hydrocarbons

A process for cracking a hydrocarbon fraction boiling in the range 400-850 DEG F. comprises use of a catalyst containing (a) nickel, tungsten or compounds thereof; (b) an acidic inorganic oxide in amorphous form selected from SiO2, Al2O3, MgO, ZrO2, or mixtures; and (c) a crystalline zeolite. Typical cracking conditions are: pressure 500-10,000 p.s.i.g.; Hydrogen rate 1000-20,000 SCF/B.; space velocity 0.1-10v./v./hr. Comparative examples describe the cracking of gas oil.ALSO:A hydrocarbon conversion catalyst comprises a crystalline zeolite and an amorphous acidic in-organic oxide of SiO2, Al2O3, MgO, ZrO2 or mixtures which support a metal or compound thereof selected from nickel, tungsten or compounds thereof. Zeolites A, D, X, Y, inordenite, charazite and analcite are specified. Preferred compounds of Ni and W are the oxides and sulphides.

Exhaust system for a vehicular positive ignition internal combustion engine

Catalytically upgrading sulphur rich naphtha

Physically stable alumino-silicate zeolite catalysts

An aluminosilicate zeolite is stabilized by calcining at 350-1200 DEG F. in air or an inert gas, e.g. H2 or He, containing >10-50% water. The zeolite may be natural, e.g. fanjasite or mordenite, or synthetic, of formula 0.7-1.1 M2/nO.Al2O3.2.2-14 SiO2, where M is alkali metal; NH4, CO, Ni, Zn, Mg, Ca, Cd, Cu, or Ba (obtained by ion-exchange of the Na form); or H (obtained by calcining the NH4 form). It may, after the calcination, be impregnated with a Pt group metal, e.g. Pd; Co, Fe, Ni, Cu, Ag, Au, Mo, W, V, Zr, Ca, Mg, Hg, Pb or a rare earth metal, or compound thereof. The preparation of 13<\>rA fanjasite from NaOG, Na aluminate, and SiO2 sol is described (Example 1) which was exchanged with a solution of NH4Cl and NH4(OH) (Example 2), dried, and calcined for 16 hours at 650 DEG F. and 2 hours at 950 DEG F. in air containing 16% water (Example 4).

Improvements in catalysts

Catalyst compositions comprise a crystalline molecular sieve having sorbed therein an organic tin compound. The catalysts may be prepared by heating the molecular sieve to drive off substantially all the water of hydration and placing the activated molecular sieve and the organic tin compound in a vacuum desiccator. The tin compound may be a compound of formula R3SnX, R4Sn, R2SnX2, RSnX3, R2SnY, RSnOOR1, R(SnOOR1)2, , or R2Sn(YRX)2 where R is a hydrocarbon or substituted hydrocarbon radical, R1 is a hydrocarbon or substituted hydrocarbon radical, hydrogen or metal, X is hydrogen, halogen, hydroxyl, amino, alkoxy, substituted alkoxy, acyloxy, substituted acyloxy, acyl or organic residues connected to tin through a sulphide link, and Y represents oxygen or sulphur; a stannous acylate; or a stannous alkoxide. Long lists of suitable tin compounds are given. The molecular sieve may be a synthesized zeolite of formula M 2/n O:Al2O3: wSiO2:yH2O where M is a cation of valence ...

Catalysed filter

A wall-flow filter monolith substrate having a porosity of at least 40% formed from a selective catalytic reduction (SCR) catalyst of extruded type.

Positive ignition engine comprising an exhaust system including a filter therefor

Filtering particulate matter from exhaust gas

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

COMPRISING ZEOLITE IN MATRIX AND CRACKING PROCESS USING SARARE EARTH METAL-CONTAINING HYDROCARBON CRACKING CATALYST ME

Gallium ion exchanged zeolites

Active gallium-ion exchanged zeolite catalysts are made by washing conventional crystalline zeolites of high silica:alumina ratio with water or acid followed by the deionised water, calcining the water-washed product and directly refluxing the calcined zeolite with a solution of a gallium compound. The gallium ion exchanged zeolites are suitable catalysts for hydro-carbon conversion reactions.

Catalyst composition

Cracking and hydrocracking of hydrocarbons may be carried out using a catalyst composition comprising crystalline aluminosilicate in an inorganic oxide matrix and prepared by subjecting a mixture comprising crystalline alkali metal aluminosilicate and inorganic oxide matrix material to steaming until the mixture contains less than 0.6 wt. per cent exchangeable alkali metal, as described in Division B1. General cracking conditions are 370 DEG to 650 DEG C., pressure from subatmospheric to several hundred atmos. In moving-bed cracking processes, reaction conditions include temperatures above 455 DEG C., pressures from sub-atmospheric to 3 atmos., catalyst: oil ratios of 1.5 to 15, LHSV of 0.5 to 6. Fluid cracking conditions include catalyst to oil ratios of 1 to 30. Examples refer to converting a gas-oil boiling range 230 DEG to 510 DEG C. to gasoline having an end-point of 210 DEG C. Hydrocracking conditions are temperatures between 204 DEG and 510 DEG C., hydrogen pressure 100 to 3000 p.s.i.g ...

PREPARATION AND USE OF METAL-CONTAINING ZEOLITIC CATALYSTS

HYDROCRACKING CATALYST

... 1348137 Hydrocracking catalysts SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ NV 23 Dec 1970 [29 Dec 1969] 61040/70 Heading B1E [Also in Division C5] Hydrocracking catalysts consists of (a) crystalline aluminasilicate zeolite having a silica:alumina moler ratio of from 2:1 to 10:1 and an alkali metal content (calculated as oxide) of less than 2, preferably of from 0.04 to 1.0, weight per cent, (b) nickel and/or a compound thereof in an amount (calculated as metal) constituting from 15 to 30, preferably from 19 to 22, weight per cent of the catalyst, (c) at least one Group IIB metal and/or a compound thereof in an amount (calculated as metal) constituting from 0.05 to 6, preferably from 0.2 to 4, weight per cent of the catalyst and, optionally, (d) halogen, for example fluorine in an amount constituting up to 10 weight per cent of the catalyst. The zeolite may be natural or synthetic, for example selected from faujasite, mordenite and zeolites X, Y and L, and may have been subjected to cation ...

Molecular sieve catalyst suitable for hydrocarbon conversion processes

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

CATALYTIC CRACKING WITH REDUCED EMISSION OF NOXIOUS GASES

PROCEDURE FOR THE IMMOBILIZATION OF A HOMOGENEOUS CATALYST, AND CATALYTIC MATERIAL

PROCEDURE FOR THE CATALYTIC REDUCTION OF NO.

CONVERSION CATALYST FOR WEIGHT OF HYDROCARBONS AND PROCEDURES FOR ITS USE.

PRODUCTION OF VINYL CHLORIDE BY CATALYTIC ONES DEHYDROHALOGENIERUNG

Procedure for the catalytic transformation of hydrocarbons

ZEOLITE ZSM-5

Formed catalyst body

Gasoline sulfur reduction catalyst for fluid catalytic cracking process

Method for controlling NOx emissions in the FCCU

CATALYST FOR PURIFYING EXHAUST GAS

Production of liquid hydrocarbons

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

IMPROVED CATALYST

ZEOLITE CATALYST AND PRODUCTION OF AROMATIC HYDROCARBONS

STEAM AND HYDROGEN TREATMENT OF ZEOLITE CATALYST

Hydrothermally stable metal promoted zeolite beta for NO_X reduction

CATALYTIC CRACKING

Process for producing light olefins

LARGE PORE ZEOLITES OF CONTROLLED ACTIVITY

CATALYST FOR THE CONVERSION OF CARBON MONOXIDE

A catalyst for the conversion of carbon monoxide comprising a support having a predetermined pore size and a metal capable of forming a metal carbonyl species is described. In one embodiment, the catalyst of the present invention comprises a mordenite, beta, or faujasite support and ruthenium metal.

CATALYST TREATMENT USEFUL FOR AROMATICS CONVERSION PROCESS

HYDROCRACKING PROCESS

COMPOSITIONS AND PROCESSES FOR REDUCING NOX EMISSIONS DURING FLUID CATALYTIC CRACKING

... ²²²Compositions for reduction of NOx generated during a catalytic cracking ²process, preferably, a fluid catalytic cracking process, are disclosed. The ²compositions comprise a fluid catalytic cracking catalyst composition, ²preferably containing a Y-type zeolite, and a NOx reducing zeolite having a ²pore size ranging from about 2 to about 7.2 Angstoms and a SiO2 to Al2O3 molar ²ratio of less than about 500 and being stabilized with a metal or metal ion ²selected from the group consisting of zinc, iron and mixtures thereof. ²Preferably, the NOx reducing zeolite particles are bound with an inorganic ²binder to form a particulate composition. In the alternative, the NOx reducing ²zeolite particles are incorporated into the cracking catalyst as an integral ²component of the catalyst. Compositions in accordance with the invention ²exhibit improved effectiveness for the reduction of NOx emissions released ²from the regenerator of a fluid catalytic cracking unit operating under FCC ²process conditions ...

PROCESS FOR THE CATALYTIC CRACKING OF HYDROCARBON OILS

K 5932 The present invention relates to a process for the catalytic cracking of hydrocarbons. The hydrocarbon cracking process is effected in the presence of a zeolitic catalyst contaminated by small quantities of heavy metals and containing tin. Application to the manufacture of fuels.

HYDROTREATING CATALYST AND PROCESS

IMMOBILIZATION OF VANADIA DEPOSITED ON CATALYTIC MATERIALS DURING CARBO-METALLIC OIL CONVERSION

... of the Invention A process is disclosed for the treatment of a hydrocarbon oil feed having a significant content of metals to lighter oil products by contacting the feed under conversion conditions in a conversion zone with a catalyst containing a sacrificial trap material sufficient to immobilize Ni-V-Na compounds. Conversion conditions are such that carbonaceous material and metals are deposited on the catalyst in the conversion zone. The catalyst is regenerated in the presence of an oxygen containing gas at a temperature sufficient to remove the carbonaceous deposits, and regenerated catalyst is recycled to the conversion zone for a contact with fresh feed. The sacrificial trap material is present on the catalyst in an amount sufficient to substantially immobilize the metal compounds in the presence of oxygen containing gas at the catalyst regeneration temperature. A catalyst composition for the above conversion comprises a catalytically active alumino-silicate zeolite dispersed in an ...

SELECTIVE DEWAXING OF HYDROCARBON OIL USING SURFACE MODIFIED ZEOLITES

A method for selectively dewaxing a waxy hydrocarbon oil feedstock comprising contacting said waxy hydrocarbon oil stock in the presence of hydrogen with a zeolite (1) which has been chemically modified by reaction, under dry, anhydrous conditions, with an organosilane wherein the zeolite has some reactive sites capable of reacting with the organosilane and where said organosilane is: (a) capable of entering into the channels of the zeolite and chemically reacting with the reactive sites present therein, as well as (b) reacting with hydroxyl groups present on the external surface of said zeolite, and (2) which has been loaded with a catalytically active hydrogenating metal component; which contacting is conducted under conditions of pressure, temperature and liquid flow velocities sufficient to effect the hydrodewaxing. Preferably the organosilane modified zeolite, either before or after the deposition of the catalytic metal component may be heated to an elevated temperature in an inert ...

CATALYTIC ACTIVITY OF ALUMINOSILICATE ZEOLITES

This invention relates to a method of improving the catalytic activity of a freshly made zeolite loaded with gallium ions by first treating with steam and then with hydrogen. Steam and hydrogen treatment may be carried out before or after loading with gallium simultaneously or successively. It has been found that a combination of steam and hydrogen treatments gives high conversions of hydrocarbon feeds and high selectivity to aromatics.

HYDROCARBON CONVERSION CATALYST CONTAINING A CO OXIDATION PROMOTER

A cracking catalyst for promoting the oxidation of carbon monoxide to carbon dioxide during regeneration of the catalyst by the burning of coke therefrom, which comprises a crystalline aluminosilicate zeolite, an inorganic porous oxide matrix material and CO oxidation promoter, such as a Group VIII metal or compound thereof. The catalyst is preferably prepared by first supporting the CO oxidation promoter on an inorganic porous oxide base, such as alumina or ultra-stable variety of Y-type zeolite, and thereafter embedding the supported CO oxidation promoter and a crystalline aluminosilicate zeolite, such as rare earth metal exchanged X- or Y-type zeolite, in an inorganic porous oxide matrix material, such as silicaalumina or clay.

SWEETENING CATALYST

HYDROTREATING CATALYST COMPRISING A LAYERED CLAY-TYPE ALUMINOSILICATE COMPONENT AND A CRYSTALLINE ZEOLITIC MOLECULAR SIEVE COMPONENT,AND PROCESS USING SAID CATALYST

BASE METAL DEWAXING CATALYST

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

NOBLE METAL AND BASE METAL DEWAXING CATALYST

Methods, catalysts, and corresponding catalyst precursors are provided for performing dewaxing of diesel or distillate boiling range fractions. The dewaxing methods, catalysts, and/or catalyst precursors can allow for production of diesel boiling range fuels with improved cold flow properties at desirable yields. The catalysts and/or catalyst precursors can correspond to supported metal catalysts and/or catalyst precursors that include at least one noble metal, such as Pt, at least one Group 8-10 base metal, preferably a non-noble Group 8-10 base metal, such as Ni and/or Co along with a Group 6 metal, such as Mo and/or W as supported metals along. The support can include a zeolitic framework structure. The catalyst precursors can be formed, for example, by impregnating a support including a zeolitic framework structure with impregnation solution(s) that also includes a dispersion agent.

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

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

CORE/SHELL HYDROCARBON TRAP CATALYST AND METHOD OF MANUFACTURE

The invention provides an automotive catalyst composite that includes a catalytic material on a carrier, the catalytic material including a plurality of core-shell support particles including a core and a shell surrounding the core, wherein the core includes a plurality of particles having a primary particle size distribution d90 of up to about 5 µm, wherein the core particles include particles of one or more molecular sieves and optionally particles of one or more refractory metal oxides; and wherein the shell comprises nanoparticles of one or more refractory metal oxides, wherein the nanoparticles have a primary particle size distribution d90 in the range of about 5 nm to about 1000 nm (1 µm); and optionally, one or more platinum group metals (PGMs) on the core-shell support. The invention also provides an exhaust gas treatment system and related method of treating exhaust gas utilizing the catalyst composite.

CATALYTIC COMPOSITION FOR CO2 CONVERSION

The present invention relates to a catalytic composition comprising at least 7 different elements selected from the group consisting of the elements defined by the intersection of the second to the sixth period and the first to the sixteenth group of the periodic table of the elements, whereby technetium is excluded, and a matrix component. A method for use of the catalytic composition is also provided.

METHOD OF PROCESSING PETROLEUM DISTILLATES

The invention relates to petroleum chemistry, in particular to method for producing high-octane gasoline fractions from straight petrol distillates. The inventive method for processing petrol distillates into gasoline fractions having an end boiling point equal to or less than 195 ~C and an octane number equal to or greater than 80 according to a motor method, consists in transforming a hydrocarbon material in a presence of a porous catalyst at a temperature ranging from 200 ~C to 250 ~C, a pressure equal to or less than 2 MPa and mass rates of a hydrocarbon mixture equal to or less than 10 h-1. Ceolite having an alumosilicate composition modified by metals having silicate or alumophosphate compositions is used as a catalyst. The inventive method makes it possible to simplify the process and increase the production of high- octane gasoline fractions using the straight petrol distillates having an extended hydrocarbon composition as a feed stock, said distillates not being pre-fractionated ...

HYDROTHERMALLY STABLE MICROPOROUS MOLECULAR SIEVE CATALYST AND PREPARATION METHOD THEREOF

Disclosed are a hydrothermally stable porous molecular sieve catalyst and a preparation method thereof. The catalyst consists of a product obtained by the evaporation of water from a raw material mixture comprising a molecular sieve having a framework of Si-OH-Al-, a water- insoluble metal salt and a phosphate compound. The catalyst maintains its physical and chemical stabilities even in an atmosphere of high temperature and humidity. Accordingly, the catalyst shows excellent catalytic activity even when it is used in a severe process environment of high temperature and humidity in heterogeneous catalytic reactions, such as various oxidation/reduction reactions, including catalytic cracking reactions, isomerization reactions, alkylation reactions and esterification reactions.

HYDROCRACKING CATALYST

METHOD FOR CONTROLLING NOX EMISSIONS IN THE FCCU

... ²²²²Processes for the reduction of NO x emissions from a regeneration zone during ²a ²fluid catalytic cracking of a hydrocarbon feedstock into lower molecular ²weight ²components are disclosed. The processes comprise contacting during a fluid ²catalytic ²cracking (FCC) process where NO x emissions are released from a regeneration ²zone of a ²fluid catalytic cracking unit (FCCU) operating in a heterogeneous combustion ²mode ²under FCC conditions, a hydrocarbon feedstock with a circulating inventory of ²a FCC ²cracking catalyst and a NO x reduction composition. The NO x reduction ²composition ²comprises: (1) at least one reduced nitrogen species component having the ²ability to ²reduce the content of reduced nitrogen species to molecular nitrogen under ²reducing or ²partial burn FCC conditions and (2) at least one NO x reduction component ²having the ²ability to convert NO x to molecular nitrogen under oxidizing or full burn FCC ²²conditions. The reduced nitrogen species and the NO x reduction ...

METHOD FOR PRODUCING METAL EXCHANGED ZEOLITES BY SOLID-STATE ION EXCHANGE AT LOW TEMPERATURES

Method for the preparation of a metal-exchanged zeolites or mixtures of metal-exchanged zeolites, such as Cu-SSZ-13, Cu-ZSM-5, Cu-beta, or Fe-beta, comprising the steps of providing a dry mixture of a) one or more microporous zeotype materials that exhibit ion exchange capacity and b) one or more metal compounds; heating the mixture in a gaseous atmosphere containing ammonia to a temperature lower than 300 °C for a time sufficient to initiate and perform a solid state ion exchange of ions of the metal compound and ions of the zeolite material; and obtaining the metal-exchanged zeolitematerial.

ALUMINA BOUND CATALYST FOR SELECTIVE CONVERSION OF OXYGENATES TO AROMATICS

A catalyst composition comprising a zeolite, an alumina binder, and a Group 12 transition metal selected from Zn and/or Cd, the zeolite having a Si/Al ratio of at least about 10 and a micropore surface area of at least about 340 m2/g, the catalyst composition comprising about 50 wt% or less of the binder, based on a total weight of the catalyst composition, and having a micropore surface area of at least about 290 m2/g, a molar ratio of Group 12 transition metal to aluminum of about 0.1 to about 1.3, and at least one of: a mesoporosity of about 20 m2/g to about 120 m2/g; a diffusivity for 2,2-dimethylbutane of greater than about 1 x 10-2 sec-1 when measured at a temperature of about 120°C; and a 2,2-dimethylbutane pressure of about 60 torr (8kPa); and a combined micropore surface area and mesoporosity of at least about 380m2/g.

CATALYST FOR SELECTIVE CONVERSION OF OXYGENATES TO AROMATICS

A catalyst composition comprises a self-bound zeolite and a Group 12 transition metal selected from the group consisting of Zn, Cd, or a combination thereof, the zeolite having a silicon to aluminum ratio of at least about 10, the catalyst composition having a micropore surface area of at least about 340 m2/g, a molar ratio of Group 12 transition metal to aluminum of about 0.1 to about 1.3, and at least one of: (a) a mesoporosity of greater than about 20 m2/g; and (b) a diffusivity for 2,2-dimethylbutane of greater than about 1 x 10-2 sec-1 when measured at a temperature of about 120°C and a 2,2-dimethylbutane pressure of about 60 torr (about 8 kPa).

METHOD FOR OXYGENATE CONVERSION

Methods for organic compound conversion are disclosed. Particular methods include providing a first mixture comprising = 10.0 wt% of at least one oxygenate, based on the weight of the first mixture; contacting said first mixture in at least a first moving bed reactor with a catalyst under conditions effective to covert at least a portion of the first mixture to a product stream comprising water, hydrogen, and one or more hydrocarbons; and separating from said product stream (i) at least one light stream and ii) at least one heavy stream, wherein the method is characterized by a recycle ratio of = 5Ø ...

CATALYST AND METHOD OF MANUFACTURE

A catalyst system comprising a first catalytic composition comprising, (i) a first component comprising a zeolite, and (ii) a second component comprising a homogeneous solid mixture containing at least one catalytic metal and at least one metal inorganic network; wherein the pores of the solid mixture have an average diameter in a range of about 1 nanometer to about 15 nanometers; wherein the first component and the second component form an intimate mixture. The catalyst system may further comprise a second catalytic composition and a third catalytic composition. The catalyst system may further comprise a delivery system configured to deliver a reductant and optionally a co-reductant. An exhaust system comprising the catalyst systems described herein is also provided.

CATALYST AND METHOD OF MANUFACTURE

A catalyst system comprising a first catalytic composition comprising a first catalytic material disposed on a metal inorganic support; wherein the metal inorganic support has pores; and at least one promoting metal. The catalyst system further comprises a second catalytic composition comprising, (i) a zeolite, or (ii) a first catalytic material disposed on a first substrate, the first catalytic material comprising an element selected from the group consisting of tungsten, titanium, and vanadium. The catalyst system may further comprise a third catalytic composition. The catalyst system may further comprise a delivery system configured to deliver a reductant and optionally a co-reductant. A catalyst system comprising a first catalytic composition, the second catalytic composition, and the third catalytic composition is also provided. An exhaust system comprising the catalyst systems described herein is also provided.

PROCESS FOR MAKING IMPROVED ZEOLITE CATALYSTS FROM PEPTIZED ALUMINAS

This invention relates to a process of preparing a catalyst from zeolite and peptized alumina. The invention comprises adding a yttrium compound to the zeolite, either prior to, during, or after its combination with the peptized alumina. The yttrium compound can be added to the zeolite via exchange of yttrium onto the zeolite prior to addition of peptized alumina, or the yttrium can be added as a soluble salt during the combination of the zeolite and peptized alumina. In either embodiment, the zeolite catalyst is then formed from the zeolite, yttrium and peptized alumina, optionally containing other inorganic oxide. This invention is suitable for preparing fluid cracking catalysts.

THERMALLY STABLE NOBLE METAL-CONTAINING ZEOLITE CATALYST

F-5673 THERMALLY STABLE NOBLE METAL-CONTAINING ZEOLITE CATALYST A zeolite catalyst composition having increased resistance to agglomeration and/or migration of its noble metal component at high temperatures and a method for preparing the catalyst composition are disclosed. The zeolite catalyst composition contains a non-framework multivalent metal oxide to stabilize the noble metal. The multivalent metal oxide, such as alumina, can be introduced into the zeolite component by diffusion, impregnation, ion-exchange, and/or calcination.

FLUIDIZED CRACKING CATALYST WITH IN SITU METAL TRAPS

A method is described for making a fluidized cracking catalyst having in situ highly dispersed metal traps which comprises (a) impregnating particles of a zeolite catalyst by the incipient wetness technique under sub-atmospheric conditions with a mixture of a tin compound and an antimony compound dissolved in an organic solvent, (b) stirring the impregnated catalyst in paste form while still under sub-atmospheric conditions, (c) heating the mixed catalyst in the presence of an oxygen-containing gas until dry, and repeating steps (a), (b) and (c) above until a desired level of said metals in the metal traps is achieved. In the incipient wetness technique, an appropriate amount of solvent is added to achieve proper transport of organometallic components, precursors of the metal traps, providing at the same time complete wetness of a given amount of catalyst without forming a layer of liquid on top of the catalyst. The impregnation procedure is usually repeated at least four times to obtain ...

Multiple zeolite catalyst

The multiple zeolite catalyst is a catalytic composition used to convert C 9+ alkylaromatic hydrocarbons to BTX, particularly commercially valuable xylenes. The catalyst is formed by mixing at least two zeolites selected from mordenite, beta zeolite, ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, MFI topology zeolite, NES topology zeolite, EU-1, MAPO-36, SAPO-5, SAPO-11, SAPO-34, and SAPO-41, and adding at least one metal component selected from Group VIB and Group VIII of the Periodic Table of the Elements. The two zeolites should have different physical and chemical characteristics, such as pore size and acidity. An exemplary catalyst includes mordenite, ZSM-5, and 3 wt. % molybdenum. The transalkylation reaction may be conducted in one or more reactors with a fixed bed, moving bed, or radial flow reactor at 200-540° C., a pressure of 1.0-5.0 MPa, and liquid hourly space velocity of 1.0-5.0 per hour.

Method for manufacturing catalyst

A method for manufacturing a catalyst, which comprises regenerating a catalyst comprising a zeolite as an active ingredient and having an ethylene conversion lowered through reaction of producing propylene by bringing into contact with ethylene in a vapor phase, by bringing the catalyst into contact with a gas which does not comprise oxygen and comprises hydrogen having a hydrogen partial pressure of 0.01 MPa or more as an absolute pressure thereof.

Double-component modified molecular sieve with improved hydrothermal stability and production method thereof

A method for producing double-component modified molecular sieve comprises adding molecular sieve to an aqueous solution containing phosphorus to form a mixture, allowing the mixture to react at pH of 1-10, temperature of 70-200° C. and pressure of 0.2-1.2 MPa for 10-200 min, and then filtering, drying and baking the resultant to obtain phosphorus-modified molecular sieve, and then adding the phosphorus-modified molecular sieve to an aqueous solution containing silver ions, allowing the phosphorus-modified molecular sieve to react with silver ions at 0-100° C. in dark condition for 30-150 min, and then filtering, drying and baking. The obtained double-component modified molecular sieve contains 88-99 wt % molecular sieve with a ratio of silica to alumina between 15 and 60, 0.5-10 wt % phosphorus (based on oxides) and 0.01-2 wt % silver (based on oxides), all based on dry matter. A catalyst produced from the double-component modified molecular sieve has improved hydrothermal stability and microactivity.

Process for making improved zeolite catalysts from peptized aluminas

This invention relates to a process of preparing a catalyst from zeolite and peptized alumina. The invention comprises adding a yttrium compound to the zeolite, either prior to, during, or after its combination with the peptized alumina. The yttrium compound can be added to the zeolite via exchange of yttrium onto the zeolite prior to addition of peptized alumina, or the yttrium can be added as a soluble salt during the combination of the zeolite and peptized alumina. In either embodiment, the zeolite catalyst is then formed from the zeolite, yttrium and peptized alumina, optionally containing other inorganic oxide. This invention is suitable for preparing fluid cracking catalysts.

Pre-carburized molybdenum-modified zeolite catalyst and use thereof for the aromatization of lower alkanes

The present invention relates to a method for producing a zeolite catalyst useful for aromatization of a lower alkane, a zeolite catalyst useful for aromatization of a lower alkane obtainable by said method and a process for aromatization of a lower alkane using the zeolite catalyst of the present invention.

Dehydrogenation of alkanols to increase yield of aromatics

The present invention provides methods, reactor systems, and catalysts for increasing the yield of aromatic hydrocarbons produced while converting alkanols to hydrocarbons. The invention includes methods of using catalysts to increase the yield of benzene, toluene, and mixed xylenes in the hydrocarbon product.

Catalyst for producing monocyclic aromatic hydrocarbons and production method of monocyclic aromatic hydrocarbons

The catalyst for producing monocyclic aromatic hydrocarbons is for producing monocyclic aromatic hydrocarbons having 6 to 8 carbon number from oil feedstock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower. The catalyst includes crystalline aluminosilicate, phosphorus, and a binder, and the amount of phosphorus is 0.1 to 10 mass % based on the total mass of the catalyst.

METHODS FOR PRODUCING MULTIFUNCTIONAL CATALYSTS FOR UPGRADING PYROLYSIS OIL

A method of making a multifunctional catalyst for upgrading pyrolysis oil includes contacting a zeolite support with a solution including at least a first metal catalyst precursor and a second metal catalyst precursor, the first metal catalyst precursor, the second metal catalyst precursor, or both, including a heteropolyacid. Contacting the zeolite support with the solution deposits or adsorbs the first metal catalyst precursor and the second catalyst precursor onto outer surfaces and pore surfaces of the zeolite support to produce a multifunctional catalyst precursor. The method further includes removing excess solution from the multifunctional catalyst precursor and calcining the multifunctional catalyst precursor to produce the multifunctional catalyst comprising at least a first metal catalyst and a second metal catalyst deposited on the outer surfaces and pore surfaces of the zeolite support. 110-. (canceled)11. A multifunctional catalyst produced by a method of making a multifunctional catalyst for upgrading pyrolysis oil , the method comprising:contacting a zeolite support with a solution comprising at least a first metal catalyst precursor and a second metal catalyst precursor, the first metal catalyst precursor, the second metal catalyst precursor, or both, comprising a heteropolyacid, where the contacting deposits the first metal catalyst precursor and the second metal catalyst precursor onto outer surfaces and pore surfaces of the zeolite support to produce a multifunctional catalyst precursor;removing excess solution from the multifunctional catalyst precursor; andcalcining the multifunctional catalyst precursor to produce the multifunctional catalyst comprising at least a first metal catalyst and a second metal catalyst deposited on the outer surfaces and pore surfaces of the zeolite support.12. The multifunctional catalyst of claim 11 , in which the first metal catalyst comprises molybdenum and the second metal catalyst comprises cobalt.13. The ...

METHODS FOR PRODUCING MULTIFUNCTIONAL CATALYSTS FOR UPGRADING PYROLYSIS OIL

A method of making a multifunctional catalyst for upgrading pyrolysis oil includes contacting a zeolite support with a solution including at least a first metal catalyst precursor and a second metal catalyst precursor, the first metal catalyst precursor, the second metal catalyst precursor, or both, including a heteropolyacid. Contacting the zeolite support with the solution deposits or adsorbs the first metal catalyst precursor and the second catalyst precursor onto outer surfaces and pore surfaces of the zeolite support to produce a multifunctional catalyst precursor. The method further includes removing excess solution from the multifunctional catalyst precursor and calcining the multifunctional catalyst precursor to produce the multifunctional catalyst comprising at least a first metal catalyst and a second metal catalyst deposited on the outer surfaces and pore surfaces of the zeolite support. 110-. (canceled)11. A multifunctional catalyst produced by a method of making a multifunctional catalyst for upgrading pyrolysis oil , the method comprising:contacting a zeolite support with a solution comprising at least a first metal catalyst precursor and a second metal catalyst precursor, the first metal catalyst precursor, the second metal catalyst precursor, or both, comprising a heteropolyacid, where the contacting deposits the first metal catalyst precursor and the second metal catalyst precursor onto outer surfaces and pore surfaces of the zeolite support to produce a multifunctional catalyst precursor;removing excess solution from the multifunctional catalyst precursor; andcalcining the multifunctional catalyst precursor to produce the multifunctional catalyst comprising at least a first metal catalyst and a second metal catalyst deposited on the outer surfaces and pore surfaces of the zeolite support.12. The multifunctional catalyst of claim 11 , in which the first metal catalyst comprises molybdenum and the second metal catalyst comprises cobalt.13. The ...

POROUS DECONTAMINATION REMOVAL COMPOSITION

The present disclosure provides enhanced zeolites and methods of making and using same. 1. An enhanced zeolite comprising zeolite and metal oxide ,wherein the metal oxide is lanthanum oxide, magnesium oxide, iron oxide, or mixed metal oxides including one or more lanthanides, the metal oxide being in the form of a nanomaterial;wherein the enhanced zeolite is stable below about pH 4; andwherein the enhanced zeolite is stable above about pH 10.2. (canceled)3. (canceled)4. (canceled)5. The enhanced zeolite of claim 1 , wherein the enhanced zeolite is stable at about 450° C.6. The enhanced zeolite of claim 1 , wherein the enhanced zeolite may be regenerated at least about 6 times.7. The enhanced zeolite of claim 6 , wherein the enhanced zeolite may be regenerated at least about 10 times.8. A method of removing phosphorous from water or wastewater comprising contacting the water or wastewater with the enhanced zeolite of .9. A method of removing phosphorous from water or wastewater comprising passing the water or wastewater through a column filter comprising the enhanced zeolite of .10. A method of removing phosphorous from water or wastewater comprising absorbing phosphorous from the water or wastewater with a permeable or semi-permeable fabric comprising the enhanced zeolite of .11. (canceled)12. (canceled)13. A method of regenerating the enhanced zeolite of any claim 1 , comprising:(a) removing phosphorous from lanthanum phosphate in a solution comprising the enhanced zeolite;(b) oxidizing lanthanum in the solution comprising the enhanced zeolite;(c) precipitating phosphorous from the solution; and(d) separating the precipitated phosphorous in step (b) from the solution.14. (canceled)15. A method of manufacturing an enhanced zeolite claim 1 , comprising:(a) mixing a precursor zeolite into a mixture of a solution of a metal salt and a first alcohol,wherein the metal salt comprises a lanthanum salt;(b) stirring the mixture at a temperature greater than about 60° C.; and ...

CATALYST AND METHOD FOR AROMATIZATION OF C3-C4 GASES, LIGHT HYDROCARBON FRACTIONS AND ALIPHATIC ALCOHOLS, AS WELL AS MIXTURES THEREOF

The invention relates to hydrocarbon feedstock processing technology, in particular, to catalysts and technology for aromatization of C-Chydrocarbon gases, light low-octane hydrocarbon fractions and oxygen-containing compounds (C-Caliphatic alcohols), as well as mixtures thereof resulting in producing an aromatic hydrocarbon concentrate (AHCC). The catalyst comprises a mechanical mixture of 2 zeolites, one of which is characterized by the silica/alumina ratio SiO/AlO=20, pre-treated with an aqueous alkali solution and modified with oxides of rare-earth elements used in the amount from 0.5 to 2.0 wt % based on the weight of the first zeolite. The second zeolite is characterized by the silica/alumina ratio SiO/AlO═82, comprises sodium oxide residual amounts of 0.04 wt % based on the weight of the second zeolite, and is modified with magnesium oxide in the amount from 0.5 to 5.0 wt % based on the weight of the second zeolite. Furthermore, the zeolites are used in the weight ratio from 1.7:1 to 2.8:1, wherein a binder comprises at least silicon oxide and is used in the amount from 20 to 25 wt % based on the weight of the catalyst. The process is carried out using the proposed catalyst in an isothermal reactor without recirculation of gases from a separation stage, by contacting a fixed catalyst bed with a gaseous feedstock, which was evaporated and heated in a preheater. The technical result consists in achieving a higher aromatic hydrocarbon yield while ensuring almost complete conversion of the HC feedstock and oxygenates, an increased selectivity with respect to forming xylols as part of an AHCC, while simultaneously simplifying the technological setup of the process by virtue of using a reduced (inter alia, atmospheric) pressure. 14-. (canceled)5. A catalyst for the aromatization of mixtures of hydrocarbons and aliphatic alcohols , the catalyst comprising: a mixture of a first pentasil zeolite and a second pentasil zeolite; the first pentasil zeolite comprising a ...

FCC CATALYST COMPOSITIONS CONTAINING BORON OXIDE AND PHOSPHORUS

A method of cracking a hydrocarbon feed under fluid catalytic cracking conditions includes adding FCC compatible inorganic particles having a first particle type including one or more boron oxide components and a first matrix component into a FCC unit and adding cracking microspheres having a second particle type including a second matrix component, a phosphorus component and 20% to 95% by weight of a zeolite component into the FCC unit. 1. A method of cracking a hydrocarbon feed under fluid catalytic cracking conditions , the method comprising adding FCC compatible inorganic particles comprising a first particle type comprising one or more boron oxide components and a first matrix component into a FCC unit and adding cracking microspheres comprising a second particle type comprising a second matrix component , a phosphorus component and 20% to 95% by weight of a zeolite component into the FCC unit.2. The method of claim 1 , wherein the one or more boron oxides present in the FCC composition is in the in the range of 0.005% to 8% by weight on an oxide basis and the phosphorus content is present on the cracking microspheres in the range of 0.5% and 10.0% by weight on an oxide basis.3. The method of claim 2 , wherein the cracking microspheres further comprise a rare earth component selected from the group consisting of yttria claim 2 , ceria claim 2 , lanthana claim 2 , praseodymia claim 2 , neodymia claim 2 , and combinations thereof.4. The method of claim 3 , wherein the rare earth component is lanthana claim 3 , and the lanthana is present in a range of 0.5 wt. % to about 10.0 wt. % on an oxide basis based on the weight of the FCC catalyst composition.5. The method of claim 4 , wherein the cracking microspheres further comprise a transition alumina component present in a range of 1 wt. % to 35 wt. %.6. The method of claim 1 , wherein the first particle type does not incorporate a zeolite.7. The method of claim 1 , wherein the one or more boron oxide components are ...

METHOD FOR TREATING ENGINE EXHAUST BY USE OF HYDROTHERMALLY STABLE, LOW-TEMPERATURE NOx REDUCTION NH3-SCR CATALYSTS

A catalyst composition includes a heterobimetallic zeolite characterized by a chabazite structure loaded with copper ions and at least one trivalent metal ion other than Al 3+ . The catalyst composition decreases NO x emissions in diesel exhaust and is suitable for operation in a catalytic converter.

Coating for reducing nitrogen oxides

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

FUEL ADDITIVE AND METHOD OF PREPARING THE SAME

Disclosed is a fuel additive which may remove varnish precursor species in a jet fuel. In particular, the fuel additive may be a multi-functional adsorbent which includes a 2-dimensional or 3-dimensional interconnected mesoporous or mixed micro-/mesoporous framework and a plurality of internal cavities formed in the mesoporous or mixed micro-/mesoporous framework and the internal cavities include charged sites to accommodate fuel contaminants for varnish formation, such as metal ions and heteroatomic contaminants. In addition, methods of preparing the multi-functional adsorbent and methods for removing varnish precursor species with the fuel additive are provided. 1. A multi-functional adsorbent for jet fuel , comprising:a 2-dimensional or 3-dimensional interconnected mesoporous or mixed micro-/mesoporous framework; anda plurality of internal cavities formed in the mesoporous or mixed micro-/mesoporous framework,wherein the internal cavities include positively charged sites, negatively charged sites or combinations thereof.2. The multi-functional adsorbent of claim 1 , wherein the mesoporous or mixed micro-/mesoporous framework is formed of a zeolite claim 1 , aluminophosphate claim 1 , hydrotalcite claim 1 , silicate clay claim 1 , alumina claim 1 , transition metal oxides claim 1 , doped variations thereof claim 1 , or combinations thereof.3. The multi-functional adsorbent of claim 1 , wherein the size of each internal cavity of the mesoporous or mixed micro-/mesoporous framework is in a range from about 0.3 nm to about 4 nm.4. The multi-functional adsorbent of claim 1 , wherein the mesoporous or mixed micro-/mesoporous framework includes a polynuclear cluster claim 1 , wherein the polynuclear cluster contains one or more positively charged or negatively charged sites.5. The multi-functional adsorbent of claim 4 , wherein the polynuclear cluster is an Alcluster claim 4 , {[AlO(OH)(HO)]·nCl} claim 4 , a polyoxometalate {[XMO]·mH}or combinations thereof claim 4 ,{' ...

Exhaust Gas Purifying Catalyst

This exhaust gas purifying catalyst is provided with a substrate and a catalyst layer formed on a surface of the substrate. The catalyst layer contains zeolite particles that support a metal, and a rare earth element-containing compound that contains a rare earth element. The rare earth element-containing compound is added in such an amount that the molar ratio of the rare earth element relative to Si contained in the zeolite is 0.001 to 0.014 in terms of oxides. 1. An exhaust gas purifying apparatus which is disposed in an exhaust pathway of an internal combustion engine and cleans exhaust gas emitted from the internal combustion engine , the apparatus comprising:an exhaust gas purifying catalyst comprising a substrate and a catalyst layer formed on a surface of the substrate, anda reducing agent supply mechanism which supplies a reducing agent for generation of ammonia to the exhaust gas at a position upstream in the exhaust pathway as compared to a position of the exhaust gas purifying catalyst, whereinthe catalyst layer contains zeolite particles that support a metal and that support a rare earth element-containing compound that contains lanthanum (La) as a rare earth element, andan amount of the rare earth element-containing compound contained is such an amount that a molar ratio of the rare earth element relative to Si contained in the zeolite particles is 0.001 to 0.014 in terms of oxides, whereinthe rare earth element-containing compound is disposed on a surface of the zeolite particles.2. The exhaust gas purifying apparatus according to claim 1 , wherein a relationship between an average particle diameter D1 of the zeolite particles and an average particle diameter D2 of the rare earth element-containing compound satisfies the following formula: 0.005<(D2/D1)<0.5.3. The exhaust gas purifying apparatus according to claim 1 , wherein an average particle diameter D2 of the rare earth element-containing compound is 100 nm or less.4. The exhaust gas purifying ...

Exhaust Gas Purifying Catalyst

This exhaust gas purifying catalyst is provided with a substrate and a catalyst layer formed on a surface of the substrate. The catalyst layer contains zeolite particles that support a metal, and a rare earth element-containing compound that contains a rare earth element. The rare earth element-containing compound is added in such an amount that the molar ratio of the rare earth element relative to Si contained in the zeolite is 0.001 to 0.014 in terms of oxides. 1. A catalyst body which is used in an exhaust gas purifying catalyst , the catalyst body comprising:zeolite particles;a metal supported on the zeolite particles; anda rare earth element-containing compound disposed on a surface of the zeolite particles, whereinthe rare earth element-containing compound contains lanthanum (La) as a rare earth element, andan amount of the rare earth element-containing compound is such an amount that a molar ratio of the rare earth element relative to Si contained in the zeolite particles is 0.001 to 0.014 in terms of oxides.21221. The catalyst body according to claim 1 , wherein a relationship between an average particle diameter D of the zeolite particles and an average particle diameter D of the rare earth element-containing compound satisfies the following formula: 0.005<(D/D)<0.5.32. The catalyst body according to claim 1 , wherein an average particle diameter D of the rare earth element-containing compound is 100 nm or less.4. The catalyst body according to claim 1 , wherein when an amount of the rare earth element at a cross section of a zeolite particle is measured using an Electron Probe Micro Analyzer (EPMA) claim 1 , the amount of the rare earth element present at the surface of the zeolite particle is greater than the amount of the rare earth element present in the inner part of the zeolite particle.5. The catalyst body according to claim 1 , wherein the rare earth element-containing compound contains at least one of lanthanum oxide and lanthanum hydroxide.6. The ...

STRONTIUM-EXCHANGED CLINOPTILOLITE

[Problem] To provide a strontium ion-exchanged clinoptilolite having excellent nitrogen-absorbing properties; and a method for producing the strontium ion-exchanged clinoptilolite. 1. A synthetic clinoptilolite comprising strontium ions at ion exchange sites thereof.2. The synthetic clinoptilolite according to claim 1 , wherein at least 35 mol % of ions at the ion exchange sites are strontium ions.3. The synthetic clinoptilolite according to claim 1 , wherein the synthetic clinoptilolite has a pore volume (pv) of 0.5 mL/g or more (pv≧0.5 mL/g) for pores having pore diameters (pd) of 3 nm≦pd≦10 claim 1 ,000 nm.4. The synthetic clinoptilolite according to claim 1 , wherein the synthetic clinoptilolite has an average pore diameter (apd) of 200 nm or larger (apd≧200 nm).5. A method for producing the synthetic clinoptilolite according to claim 1 , comprising bringing the synthetic clinoptilolite into contact with a solution containing strontium under ambient pressure to undergo ion exchange.6. The method for producing the synthetic clinoptilolite according to claim 5 , wherein the synthetic clinoptilolite is a clinoptilolite obtained by: [{'br': None, 'sub': 2', '2', '3, '8≦SiO/AlO≦20,'}, {'br': None, 'sub': '2', '0.25≦OH/SiO≦0.5,'}, {'br': None, '0.5≦K/(K+Na)≦0.9, and'}, {'br': None, 'sub': 2', '2, '10≦HO/SiO≦100 in terms of the molar ratio; and'}], 'mixing an amorphous aluminosilicate gel obtained from an alkaline silicate and an aluminum salt, an alkali metal hydroxide, and water to provide a mixture satisfyingstirring the obtained mixture in the presence of a seed crystal to undergo crystallization at temperatures (ct) of 100° C.≦ct≦200° C.7. A synthetic clinoptilolite molding body containing the synthetic clinoptilolite according to .8. A nitrogen adsorbent containing synthetic clinoptilolite according to . The present invention relates to a strontium ion-exchanged clinoptilolite.Clinoptilolite, one of common naturally yielding zeolites, has been industrially used ...

METHOD OF PREPARING AN STT-TYPE ZEOLITE FOR USE AS A CATALYST IN SELECTIVE CATALYTIC REDUCTION REACTIONS

A method of preparing a crystalline STT-type zeolite that has a mole ratio greater than about 15:1 of a tetravalent element oxide to a trivalent element oxide is disclosed along with a gas treatment system that incorporates the STT-type zeolite and a process for treating a gas using the STT-type zeolite. The method generally comprises forming an aqueous mixture comprising a tetravalent element oxide source, a trivalent element oxide source, a source of alkali metal, and an organic structure directing agent; maintaining the mixture under conditions that crystallize crystals of a STT-type zeolite; and recovering the crystals The STT-type zeolite crystals exhibit x-ray diffraction 2-theta degree peaks at: 8.26, 8.58, 9.28, 9.54, 10.58, 14.52, 15.60, 16.43, 17.13, 17.74, 18.08, 18.46, 19.01, 19.70, 20.12, 20.38, 20.68, 21.10, 21.56, 22.20, 22.50, 22.78, 23.36, 23.76, 23.99, 24.54, 24.92, 25.16, 25.58, 25.80, 26.12, 26.94, 27.38, 27.92, 28.30, 28.60, 29.24, 29.48, 30.08, 30.64, 31.20, 31.46, 31.80, 32.02, 32.60, 33.60, and 34.43. 1. A method for preparing a crystalline STT-type zeolite , having a mole ratio greater than about 15:1 of an oxide of a tetravalent element to an oxide of a trivalent element , said method comprising:forming an aqueous reaction mixture comprising a source of the oxide of tetravalent element; a source of the oxide of the trivalent element; a source of alkali metal; an organic structure directing agent comprising N,N,N-trimethyl-1-adamantamonium hydroxide;maintaining the aqueous reaction mixture under crystallization conditions sufficient to crystallize crystals of a STT-type zeolite having an x-ray diffraction pattern with 2 theta peaks at: 8.26, 8.58, 9.28, 9.54, 10.58, 14.52, 15.60, 16.43, 17.13, 17.74, 18.08, 18.46, 19.01, 19.70, 20.12, 20.38, 20.68, 21.10, 21.56, 22.20, 22.50, 22.78, 23.36, 23.76, 23.99, 24.54, 24.92, 25.16, 25.58, 25.80, 26.12, 26.94, 27.38, 27.92, 28.30, 28.60, 29.24, 29.48, 30.08, 30.64, 31.20, 31.46, 31.80, 32.02, 32.60, ...

Method of Forming a Catalyst with an Ion-Modified Binder

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

Exhaust gas purifying catalyst

This exhaust gas purifying catalyst is provided with a substrate 10 and a catalyst layer 20 formed on a surface of the substrate 10 . The catalyst layer 20 contains zeolite particles 22 that support a metal, and a rare earth element-containing compound 24 that contains a rare earth element. The rare earth element-containing compound 24 is added in such an amount that the molar ratio of the rare earth element relative to Si contained in the zeolite 22 is 0.001 to 0.014 in terms of oxides.

Copper cha zeolite catalysts

Zeolite catalysts and systems and methods for preparing and using zeolite catalysts having the CHA crystal structure are disclosed. The catalysts can be used to remove nitrogen oxides from a gaseous medium across a broad temperature range and exhibit hydrothermal stable at high reaction temperatures. The zeolite catalysts include a zeolite carrier having a silica to alumina ratio from about 15:1 to about 256:1 and a copper to alumina ratio from about 0.25:1 to about 1:1.

MOLYBDENUM BASED CATALYST SUPPORTED ON TITANIA-MODIFIED ZEOLITE

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

LOWER-HYDROCARBON AROMATIZATION CATALYST AND METHOD FOR PRODUCING LOWER-HYDROCARBON AROMATIZATION CATALYST

To contribute to the improvement of catalytic activity of a lower hydrocarbon aromatization catalyst, which converts a lower hydrocarbon(s) to an aromatic compound(s), and to the improvement of compactability of the catalyst. 17-. (canceled)8. A lower hydrocarbon aromatization catalyst characterized by being formed by compacting a catalyst-supported , metallosilicate mixture of a first metallosilicate having a catalyst metal supported on a metallosilicate having a Si/Al ratio of 10-100 and a second metallosilicate supporting thereon the catalyst metal , having a Si/Al ratio of 10-100 , and having an average grain size smaller than that of the first metallosilicate.9. The lower hydrocarbon aromatization catalyst according to claim 8 , which is characterized by that the average grain size of the second metallosilicate is one fifth or less of that of the first metallosilicate.10. The lower hydrocarbon aromatization catalyst according to claim 9 , which is characterized by that the average grain size of the first metallosilicate is from 1.0 μm to 5.0 μm.11. The lower hydrocarbon aromatization catalyst according to claim 9 , which is characterized by that the average grain size of the second metallosilicate is from 0.1 μm to 1.0 μm.12. The lower hydrocarbon aromatization catalyst according to claim 8 , which is characterized by that the second metallosilicate is added by from 20% to 80% claim 8 , relative to mass of the mixture.13. A process for producing a lower hydrocarbon aromatization catalyst for converting a lower hydrocarbon to an aromatic compound and is characterized bythat a first metallosilicate having a Si/Al ratio of 10-100, on which a catalyst metal is to be supported, and a second metallosilicate having an average grain size smaller than that of the first metallosilicate and having a Si/Al ratio of 10-100 are mixed together,that the metal catalyst is supported on a mixture obtained by the mixing, andthat this catalyst metal supported mixture is compacted. ...

PROCESSES FOR REFORMING AND TRANSALKYLATING HYDROCARBONS

Processes for reforming and transalkylating hydrocarbons are disclosed. A method for processing a hydrocarbon stream includes the steps of separating para-xylene from a first mixed-xylene and ethylbenzene-containing stream to produce a first non-equilibrium xylene and ethylbenzene stream and isomerizing the first non-equilibrium xylene and ethylbenzene stream to produce additional para-xylene. The method further includes transalkylating a toluene stream to produce a second mixed-xylene and ethylbenzene-containing stream, separating para-xylene from the second mixed-xylene and ethylbenzene-containing stream to produce a second non-equilibrium xylene and ethylbenzene stream, and isomerizing the second non-equilibrium xylene and ethylbenzene stream using a liquid phase isomerization process to produce additional para-xylene. 1. A process for processing a hydrocarbon stream comprising the steps of:separating para-xylene from the first mixed-xylene and ethylbenzene-containing stream to produce a first non-equilibrium xylene and ethylbenzene stream;isomerizing the first non-equilibrium xylene and ethylbenzene stream to produce additional para-xylene;transalkylating a toluene stream to produce a second mixed-xylene and ethylbenzene-containing stream;separating para-xylene from the second mixed-xylene and ethylbenzene-containing stream to produce a second non-equilibrium xylene and ethylbenzene stream; andisomerizing the second non-equilibrium xylene and ethylbenzene stream using a liquid phase isomerization process to produce additional para-xylene.2. The process of claim 1 , wherein the first mixed-xylene and ethylbenzene-containing stream comprises a greater proportion of ethylbenzene than does the second mixed-xylene and ethylbenzene-containing stream.3. The process of claim 1 , further comprising reforming a naphtha-containing hydrocarbon stream to produce the first mixed-xylene and ethylbenzene-containing stream and the toluene stream.4. The process of claim 3 , ...

GD-CONTAINING, ANTI-COKING SOLID ACID CATALYSTS AND PREPARATION METHOD AND USE THEREOF

The present invention relates to an anti-coking catalyst having a physical property of reducing coke formation, which comprises a solid acid catalyst containing gadolinium (Gd) on the surface, a preparation method thereof, and a use thereof. The preparation method includes a first step of determining the amount of gadolinium (Gd) or a Gd-providing precursor to be used relative to the total weight of the solid acid catalyst, which reduces the coking of a specific solid acid catalyst below a specific level under a specific reaction condition; and a second step of preparing a Gd-containing solid acid catalyst using the amount determined in the first step. 1. A method of preparing an anti-coking solid acid catalyst having a physical property of reducing coke formation , comprising:a first step of determining the amount of gadolinium (Gd) or Gd-providing precursor to be used relative to the total weight of the solid acid catalyst, which reduces the coking of a specific solid acid catalyst below a specific level under a specific reaction condition in which the catalyst is intended to be used; anda second step of preparing a Gd-containing solid acid catalyst using the amount determined in the first step.2. The method according to claim 1 , wherein the Gd-containing solid acid catalyst prepared in the second step has an increased number of a base site of the solid acid catalyst by the presence of gadolinium.3. The method according to claim 1 , wherein the Gd-containing solid acid catalyst prepared in the second step has a film containing Gd metal or gadolinium oxide formed on the surface of the solid acid catalyst with a nano-size thickness.4. The method according to claim 1 , wherein the amount of gadolinium to be used relative to the total weight of the solid acid catalyst is determined from the temperature-programmed desorption curve of carbon dioxide claim 1 , base strength claim 1 , or base site density per gadolinium content.5. The method according to claim 1 , ...

CATALYST WITH IMPROVED ACTIVITY/SELECTIVITY FOR LIGHT NAPHTHA AROMATIZATION

In an embodiment, A catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the catalyst has an Si:Almole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5; wherein the catalyst has an aluminum content of less than or equal to 0.75 wt %; wherein the catalyst is non-acidic. 1. A catalyst comprising:a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the zeolite is a medium pore zeolite having an average pore size of 5 to 8 Å;{'sub': '2', 'wherein the catalyst has an Si:Almole ratio of 125 to 211, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5;'}wherein the catalyst has an aluminum content of less than or equal to 0.75 wt %, and a Ge content of 0.1 to 3 wt %, based on the total weight of the catalyst excluding any binder and extrusion aide;wherein the catalyst is non-acidic.2. The catalyst of claim 1 , wherein the Ge is present in an amount of 0.4 to 2.5 wt % claim 1 , and/or the Na is present in an amount of 0.5 to 2 wt % and/or the Pt is present in an amount of 0.05 to 3 wt % claim 1 , wherein the wt % values are based on the total weight of the catalyst excluding any binder and extrusion aide.3. The catalyst of claim 2 , wherein the catalyst has all of the Ge content of 0.4 to 2.5 wt % claim 2 , the Na content of 0.5 to 2 wt % claim 2 , and the Pt content of 0.05 to 3 wt % claim 2 , wherein the wt % values are based on the total weight of the catalyst excluding any binder and extrusion aide.4. The catalyst of claim 1 , wherein the catalyst has a Ge content of 0.4 to 1.5 wt % based on the total weight of the catalyst excluding any binder and extrusion aide.5. The catalyst of claim 1 , wherein the catalyst comprises Al in an amount of 0.45 to 0.7 wt % based on the total weight of the catalyst excluding any binder and extrusion aide.6. The catalyst of claim 1 , wherein the zeolite is MTW claim 1 , ...

Clean Gas Stack

A flow-through solid catalyst formed by coating a zeolite material on a metal or ceramic solid substrate. In some embodiments, the solid substrate is formed as flat plates, corrugated plates, or honeycomb blocks. 1. An apparatus for drying and cleaning stack gases from a fossil fuel source , the apparatus comprising: [{'sup': '2', 'a zeolite material with a porosity of a total surface area of not greater than 1200 m/g and effective for achieving at least 70% reduction in carbon oxides, sulfur oxides, or nitrogen oxides from the stack gases;'}, 'a metal or ceramic solid substrate to which the zeolite material has been applied to create a zeolite-coated solid substrate; and', 'spacing between components of the substrate being selected based on a flow-through capacity of, a pressure drop across, and an effectiveness of removal of carbon oxides, sulfur oxides, or nitrogen oxides by the flow-through solid catalyst; and, 'a plurality of flow-through solid catalysts, each of the plurality of flow-through solid catalysts comprisinga pair of electrodes positioned inline in a gas flow upstream of the plurality of flow-through solid catalysts, the electrodes being insulated from containment of the gas flow, with a DC voltage applied between the electrodes to ionize water vapor in the gas flow without creating substantial amounts of hydrogen gas and to reduce moisture content of the gas flow through the flow-through solid catalysts.2. The apparatus of claim 1 , the DC voltage applied between the electrodes being less than 34 volts.3. The apparatus of claim 1 , the solid substrate comprising a material selected from a group consisting of stainless steel claim 1 , copper claim 1 , titanium claim 1 , a titanium alloy claim 1 , aluminum claim 1 , cordierite claim 1 , mullite claim 1 , and alumina.4. The apparatus of claim 1 , each of the plurality of flow-through solid catalysts further comprising a binder to increase adherence of the zeolite material to the substrate.5. The ...

NOVEL METHODS FOR PRODUCING CRYSTALLINE MICROPOROUS SOLIDS WITH THE RTH TOPOLOGY AND COMPOSITIONS DERIVED FROM THE SAME

This disclosure relates to new crystalline microporous solids (including silicate- and aluminosilicate-based solids), the compositions comprising 8 and 10 membered inorganic rings, particularly those having RTH topologies having a range of Si:Al ratios, methods of preparing these and known crystalline microporous solids using certain quaternized imidazolium cation structuring agents. 1. A process for preparing a crystalline microporous solid of RTH topology , the process comprising hydrothermally treating a composition comprising: '(ii) at least one source of aluminum oxide, boron oxide, gallium oxide, hafnium oxide, iron oxide, tin oxide, titanium oxide, indium oxide, vanadium oxide, zirconium oxide, or combination or mixture thereof', '(a) (i) at least one source of silicon oxide and'}in the presence of an organic complex comprising(b) an imidazolium cation comprising methyl and ethyl groups and having a C/N+ ratio in a range of from 6:1 to 10:1; and(c) an associated hydroxide or fluoride anion;under conditions effective to crystallize the crystalline microporous solid of RTH topology.2. The process of claim 1 , comprising hydrothermally treating a composition comprising (ii) at least one source of aluminum oxide; and optionally', '(iii) at least one source of boron oxide, gallium oxide, hafnium oxide, iron oxide, tin oxide, titanium oxide, indium oxide, vanadium oxide, zirconium oxide, or combination or mixture thereof and, '(a) (i) at least one source of a silicon oxide, germanium oxide, or combination thereof;'}(b) an imidazolium cation comprising methyl and ethyl groups and having a C/N+ ratio in a range of from 6:1 to 8:1 and an associated hydroxide or fluoride anion, under conditions effective to crystallize a crystalline microporous aluminosilicate solid of RTH topology.4. The process of claim 1 , wherein the source of silicon oxide comprises a silicate claim 1 , silica hydrogel claim 1 , silicic acid claim 1 , fumed silica claim 1 , colloidal silica claim ...

Modified Crystalline Aluminosilicate for Dehydration of Alcohols

The present invention relates to a catalyst composition comprising a modified crystalline aluminosilicate of the Framework Type FER having Si/Al framework molar/ratio greater than 20 characterized in that in said modified crystalline aluminosilicate the ratio between the strong acid sites and the weak acid sites, S/W, is lower than 1.0 and having the extra framework aluminum (EFAL) content lowered to less than 10 wt % preferably 5 wt % even more preferably less than 2 wt % measured by 27Al MAS NMR. The present invention further relates to a process for producing olefins from alcohols in presence of said catalyst composition. 117.-. (canceled)19. The process for the preparation of a catalyst composition according to further characterized in that said organic acidic medium or an organic medium of step ii.){'sub': 2', '3', '4, 'comprises one or more —COH, —SOH or —SOH groups or salts thereof; or'}is chosen among citric acid, formic acid, oxalic acid, tartaric acid, malonic acid, succinic acid, glutaric acid, adipic acid, maleic acid, phthalic acid, isophthalic acid, fumaric acid, nitrilotriacetic acid, hydroxyethylenediaminetriacetic acid, ethylene di amine tetracetic acid i.e. EDTA, or their corresponding salts being sodium salts or any mixture of thereof.20. The process for the preparation of a catalyst composition according to further characterized in that a calcination is performed before step ii.) said calcination being performed at a temperature lower than 600° C. and with a temperature increase of less than 10° C./min claim 18 , preferably less than 1° C./min for a period of at least 30 min and under a gas flow containing at most 1000 ppm volume of water measured at the inlet of the calcination reactor.21. The process for the preparation of a catalyst composition according to wherein said modified crystalline aluminosilicate of the Framework Type FER has Si/Al framework molar ratio ranging from 25 to 50.22. The process for the preparation of a catalyst ...

Modified Y-Zeolite/ZSM-5 Catalyst For Increased Propylene Production

Provided is a Fluid Catalytic Cracking catalyst composition having increased propylene production with respect to other Fluid Catalytic Cracking catalysts (measured at constant conversion). The catalyst composition comprises a particulate which comprises (a) non-rare earth metal exchanged Y-zeolite in an amount in the range of about 5 to about 50 wt %, based upon the weight of the particulate; and (b) ZSM-5 zeolite in an amount in the range of about 2 to about 50 wt %, based upon the weight of the particulate.

METHOD FOR PRODUCING METAL EXCHANGED ZEOLITES BY SOLID-STATE ION EXCHANGE AT LOW TEMPERATURES

Method for the preparation of a metal-exchanged zeolites or mixtures of metal-exchanged zeolites, such as Cu-SSZ-13, Cu-ZSM-S, Cu-beta, or Fe-beta, comprising the steps of providing a dry mixture of a) one or more microporous zeotype materials that exhibit ion exchange capacity and b) one or more metal compounds; heating the mixture in a gaseous atmosphere containing ammonia to a temperature lower than 300° C. for a time sufficient to initiate and perform a solid state ion exchange of ions of the metal compound and ions of the zeolite material; and obtaining the metal-exchanged zeolitematerial. 1. Method for the preparation of a metal-exchanged zeolite material or mixtures of metal-exchanged zeolites materials comprising the steps of providing a dry mixture containing a) one or more zeolites starting materials that exhibit ion exchange capacity and b) one or more metal compounds; heating the mixture in a gaseous atmosphere containing ammonia to a temperature of up to 300° C. and for a time sufficient to initiate and perform a solid state ion exchange of ions of the metal compound and ions of the one or more zeolites; and obtaining the metal-exchanged zeolite material or the mixture of metal-exchanged zeolite materials.2. Method according to claim 1 , wherein the one or more zeolite starting materials have the framework code of AEI claim 1 , AFX claim 1 , CHA claim 1 , KFI claim 1 , LTA claim 1 , IMF claim 1 , ITH claim 1 , MEL claim 1 , MFI claim 1 , SZR claim 1 , TUN claim 1 , *BEA claim 1 , BEC claim 1 , FAU claim 1 , FER claim 1 , MOR claim 1 , LEV.3. Method according to claim 1 , wherein the one or more zeolite starting materials are selected from the group consisting of ZSM-5 claim 1 , zeolite Y claim 1 , beta zeolite claim 1 , SSZ-13 claim 1 , SSZ-39 claim 1 , SSZ-62 claim 1 , and Chabazite.4. Method according to claim 1 , wherein the one or more zeolite starting materials are in the N or NH4 form.5. Method according to claim 1 , wherein the one or more ...

Catalyst and method for aromatization of c3-c4 gases, light hydrocarbon fractions and aliphatic alcohols, as well as mixtures thereof

The invention relates to hydrocarbon feedstock processing technology, in particular, to catalysts and technology for aromatization of C 3 -C 4 hydrocarbon gases, light low-octane hydrocarbon fractions and oxygen-containing compounds (C 1 -C 3 aliphatic alcohols), as well as mixtures thereof resulting in producing an aromatic hydrocarbon concentrate (AHCC). The catalyst comprises a mechanical mixture of 2 zeolites, one of which is characterized by the silica/alumina ratio SiO 2 /Al 2 O 3 =20, pre-treated with an aqueous alkali solution and modified with oxides of rare-earth elements used in the amount from 0.5 to 2.0 wt % based on the weight of the first zeolite. The second zeolite is characterized by the silica/alumina ratio SiO 2 /Al 2 O 3 =82, comprises sodium oxide residual amounts of 0.04 wt % based on the weight of the second zeolite, and is modified with magnesium oxide in the amount from 0.5 to 5.0 wt % based on the weight of the second zeolite. Furthermore, the zeolites are used in the weight ratio from 1.7:1 to 2.8:1, wherein a binder comprises at least silicon oxide and is used in the amount from 20 to 25 wt % based on the weight of the catalyst. The process is carried out using the proposed catalyst in an isothermal reactor without recirculation of gases from a separation stage, by contacting a fixed catalyst bed with a gaseous feedstock, which was evaporated and heated in a preheater. In The technical result consists in achieving a higher aromatic hydrocarbon yield while ensuring almost complete conversion of the HC feedstock and oxygenates, an increased selectivity with respect to forming xylols as part of an AHCC, while simultaneously simplifying the technological setup of the process by virtue of using a reduced (inter alia, atmospheric) pressure.

MODIFIED ZEOLITE CATALYST AND METHODS FOR PRODUCING AND USING SAME

The invention pertains to a zeolite catalyst, methods of making same, and its use in the catalytic cracking of naphtha for the production of lower molecular weight olefins and alkanes, while minimizing production less desirable products. A zeolite is modified by base leaching and by the addition of a metal cation, thereby lowering the Si/Alratio and improving the stability of the formed catalyst. 1. A method of modifying a zeolite catalyst comprising:providing a zeolite catalyst;{'sub': 2', '3, 'contacting the provided zeolite catalyst with a first composition comprising NaOH and NaCO, thereby producing a leached zeolite catalyst;'}contacting the leached zeolite catalyst with a second composition comprising a realuminating agent, thereby producing a realuminated zeolite catalyst;modifying the provided zeolite catalyst, the leached zeolite catalyst, or the realuminated zeolite with one or more metal atoms or ions comprising Mg, Ba, Sr, Cr, Fe, Co, Ni, Cu, Zn, Ga, Ce, Ag, Pd, Bi, Ti, V, Zr, Mo, W, Li, or La, or a mixture thereof;wherein the method produces a modified zeolite catalyst.2. The method of claim 1 , wherein the realuminating agent comprises NaAlO claim 1 , KAlO claim 1 , or a combination thereof.3. The method of claim 1 , wherein the provided zeolite catalyst comprises HZSM-5.4. The method of claim 1 , wherein the provided zeolite catalyst has a Si/Alratio of 27.5. The method of claim 1 , wherein the first composition comprises 0.05 M NaOH and 0.8 M NaCO.6. The method of claim 1 , wherein the second composition comprises from 0.5 mmol to 4.0 mmol of Al per gram of leached zeolite catalyst.7. The method of claim 1 , wherein the metal atom or ion comprises Ti.8. The method of claim 1 , wherein modifying the provided zeolite catalyst claim 1 , the leached zeolite catalyst claim 1 , or the realuminated zeolite with a metal atom or ion comprises contacting the provided zeolite catalyst claim 1 , the leached zeolite catalyst claim 1 , or the realuminated zeolite ...

METAL MODIFIED Y ZEOLITE, ITS PREPARATION AND USE

The present invention relates to a metal modified Y zeolite, its preparation and use. Said zeolite contains 1-15 wt % of IVB group metal as oxide and is characterized in that the ratio of the zeolite surface's IVB group metal content to the zeolite interior's IVB group metal content is not higher than 0.2; and/or the ratio of the distorted tetrahedral-coordinated framework aluminum to the tetrahedral-coordinated framework aluminum in the zeolite lattice structure is (0.1-0.8):1.

METAL MODIFIED Y ZEOLITE, ITS PREPARATION AND USE

The present invention relates to a metal modified Y zeolite, its preparation and use. Said zeolite contains 1-15 wt % of IVB group metal as oxide and is characterized in that the ratio of the zeolite surface's IVB group metal content to the zeolite interior's IVB group metal content is not higher than 0.2; and/or the ratio of the distorted tetrahedral-coordinated framework aluminum to the tetrahedral-coordinated framework aluminum in the zeolite lattice structure is (0.1-0.8):1.

HYDROCARBON OIL DESULFURIZATION ADSORBING AGENT, PRODUCTION AND USE THEREOF

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

TRANSITION METAL/ZEOLITE SCR CATALYSTS

A method of converting nitrogen oxides in a gas to nitrogen by contacting the nitrogen oxides with a nitrogenous reducing agent in the presence of a zeolite catalyst containing at least one transition metal, wherein the zeolite is a small pore zeolite containing a maximum ring size of eight tetrahedral atoms, wherein the at least one transition metal is selected from the group consisting of Cr, Mn, Fe, Co, Ce, Ni, Cu, Zn, Ga, Mo, Ru, Rh, Pd, Ag, In, Sn, Re, Ir and Pt. 1. An exhaust system for treatment of an exhaust gas stream comprising NOand particulate matter , the exhaust system comprising:an SCR catalyst substrate containing a catalyst comprising a copper-containing, metal-substituted silicoaluminophosphate having a CHA framework structure; andan ammonia injector or an ammonia precursor injector positioned upstream of the SCR catalyst substrate;{'sub': '2', 'wherein the catalyst is effective to promote the reaction of ammonia with nitrogen oxides to form nitrogen and HO selectively.'}2. The exhaust system of claim 1 , wherein the metal-substituted silicoaluminophosphate is substituted with one or more of As claim 1 , B claim 1 , Be claim 1 , Co claim 1 , Fe claim 1 , Ga claim 1 , Ge claim 1 , Li claim 1 , Mg claim 1 , Mn claim 1 , Zn and Zr.3. The exhaust system of claim 2 , wherein the metal-substituted silicoaluminophosphate is substituted with Zr.4. The exhaust system of claim 1 , wherein the metal-substituted silicoaluminophosphate comprises metal-substituted SAPO-34.5. The exhaust system of claim 4 , wherein the metal-substituted SAPO-34 is substituted with one or more of As claim 4 , B claim 4 , Be claim 4 , Co claim 4 , Fe claim 4 , Ga claim 4 , Ge claim 4 , Li claim 4 , Mg claim 4 , Mn claim 4 , Zn and Zr.6. The exhaust system of claim 5 , wherein the metal-substituted SAPO-34 is substituted with Zr.7. The exhaust system of claim 1 , wherein the catalyst contains a binder selected from the group consisting of alumina claim 1 , silica claim 1 , (non- ...

CO2 DESORPTION CATALYST

This invention provides a COdesorption catalyst that has an excellent COdesorption activity and that can be used to replace metal filler. This invention provides a COdesorption catalyst comprising an inorganic powder or inorganic powder compact, the inorganic powder or inorganic powder compact having a BET specific surface area of 7 m/g or more. 1. A COdesorption device including:{'sub': 2', '2, 'a COabsorption tower for absorbing and removing COfrom exhaust gas by using an absorbing solution; and'}{'sub': '2', 'a regeneration tower for regenerating the absorbing solution containing absorbed CO,'}{'sub': '2', 'wherein the regeneration tower contains a COdesorption catalyst comprising an inorganic powder or inorganic powder compact,'}{'sup': '2', 'wherein the inorganic powder or inorganic powder compact has a BET specific surface area of 7 m/g or more,'}{'sub': 2', '3, 'wherein the inorganic powder or inorganic powder compact is at least one member selected from the group consisting of AlOand zeolites, and'}wherein at least one metal selected from the group consisting of Pd, Fe, Co, Ag, Ni, and Pt is supported on the catalyst.2. The COdesorption device according to claim 1 , wherein the inorganic powder or inorganic powder compact further comprises BN.3. A method for desorbing CO claim 1 ,{'sub': '2', 'the method comprising the step of regenerating an absorbing solution containing absorbed CO,'}{'sub': 2', '2, 'wherein the regeneration step brings the absorbing solution containing absorbed COinto contact with a COdesorption catalyst comprising an inorganic powder or inorganic powder compact,'}{'sup': '2', 'wherein the inorganic powder or inorganic powder compact has a BET specific surface area of 7 m/g or more,'}{'sub': 2', '3, 'wherein the inorganic powder or inorganic powder compact is at least one member selected from the group consisting of AlOand zeolites, and'}wherein at least one metal selected from the group consisting of Pd, Fe, Co, Ag, Ni, and Pt is ...

HIGH EFFICIENCY AND DURABILITY SELECTIVE CATALYTIC REDUCTION CATALYST

This disclosure features an exhaust aftertreatment system that includes a selective catalytic reduction catalyst that includes a metal oxide catalyst and a metal zeolite catalyst, a metal oxide catalyst that is other than a vanadium oxide catalyst and a vanadium oxide catalyst, or a metal oxide catalyst that is other than a vanadium oxide catalyst together with a metal zeolite catalyst and a vanadium oxide catalyst. When used in a selective catalytic reduction system in a diesel engine, the catalyst composition can increase a conversion efficiency of nitrogen oxides (NOx) to nitrogen and water by a minimum of 2 percent compared to the metal zeolite catalyst alone, the metal oxide catalyst alone, or the vanadium oxide catalyst alone, when present. 1. A selective catalytic reduction catalyst composition , comprising:a metal oxide catalyst; anda metal zeolite catalyst or a vanadium oxide catalyst,wherein the catalyst composition increases a conversion efficiency of nitrogen oxides to nitrogen and water by at least 2% compared to the metal oxide catalyst alone, the metal zeolite catalyst alone, or the vanadium oxide catalyst alone.2. The catalyst composition of claim 1 , wherein the metal oxide catalyst is selected from cerium oxide claim 1 , titanium oxide claim 1 , zirconium oxide claim 1 , aluminum oxide claim 1 , silicon oxide claim 1 , hafnium oxide claim 1 , vanadium oxide claim 1 , niobium oxide claim 1 , tantalum oxide claim 1 , chromium oxide claim 1 , molybdenum oxide claim 1 , tungsten oxide claim 1 , ruthenium oxide claim 1 , rhodium oxide claim 1 , iridium oxide claim 1 , nickel oxide claim 1 , barium oxide claim 1 , yttrium oxide claim 1 , scandium oxide claim 1 , calcium oxide claim 1 , manganese oxide claim 1 , chromium oxide claim 1 , lanthanum oxide claim 1 , strontium oxide claim 1 , cobalt oxide claim 1 , and any combination thereof.3. The catalyst composition of claim 1 , wherein the metal oxide catalyst is selected from the group consisting of ...

CORE/SHELL HYDROCARBON TRAP CATALYST AND METHOD OF MANUFACTURE

The invention provides an automotive catalyst composite that includes a catalytic material on a carrier, the catalytic material including a plurality of core-shell support particles including a core and a shell surrounding the core, wherein the core includes a plurality of particles having a primary particle size distribution dof up to about 5 μm, wherein the core particles include particles of one or more molecular sieves and optionally particles of one or more refractory metal oxides; and wherein the shell comprises nanoparticles of one or more refractory metal oxides, wherein the nanoparticles have a primary particle size distribution din the range of about 5 nm to about 1000 nm (1 μm); and optionally, one or more platinum group metals (PGMs) on the core-shell support. The invention also provides an exhaust gas treatment system and related method of treating exhaust gas utilizing the catalyst composite. 1. An automotive catalyst composite comprising:a catalytic material on a carrier, the catalytic material comprising a plurality of core-shell support particles comprising a core and a shell surrounding the core,{'sub': '90', 'wherein the core comprises a plurality of particles having a primary particle size distribution dof up to about 5 μm, wherein the core particles comprise particles of one or more molecular sieves and optionally particles of one or more refractory metal oxides; and'}{'sub': '90', 'claim-text': optionally, one or more platinum group metals (PGMs) on the core-shell support;', 'wherein the catalytic material is effective to temporarily trap hydrocarbons in a vehicle exhaust stream and thereafter release the trapped hydrocarbons and convert the hydrocarbons to carbon oxides and water., 'wherein the shell comprises nanoparticles of one or more refractory metal oxides, wherein the nanoparticles have a primary particle size distribution din the range of about 5 nm to about 1000 nm (1 μm); and'}2. The automotive catalyst composite of claim 1 , wherein ...

Copper CHA Zeolite Catalysts

Zeolite catalysts and systems and methods for preparing and using zeolite catalysts having the CHA crystal structure are disclosed. The catalysts can be used to remove nitrogen oxides from a gaseous medium across a broad temperature range and exhibit hydrothermal stable at high reaction temperatures. The zeolite catalysts include a zeolite carrier having a silica to alumina ratio from about 15:1 to about 256:1 and a copper to alumina ratio from about 0.25:1 to about 1:1. 1. A catalyst comprising: an aluminosilicate zeolite having the CHA crystal structure and a mole ratio of silica to alumina from about 15 to about 150 and an atomic ratio of copper to aluminum from about 0.25 to about 1 , the catalyst effective to promote the reaction of ammonia with nitrogen oxides to form nitrogen and HO selectively , wherein the zeolite comprises Cu-SSZ-13.2. The catalyst of claim 1 , wherein the mole ratio of silica to alumina is from about 15 to about 100.3. The catalyst of claim 2 , wherein the mole ratio of silica to alumina is from about 25 to about 40.4. The catalyst of claim 2 , wherein the mole ratio of silica to alumina is about 30.5. The catalyst of claim 2 , wherein the atomic ratio of copper to aluminum is from about 0.30 to about 0.50.6. The catalyst of claim 2 , wherein the atomic ratio of copper to aluminum is about 0.40.7. The catalyst of claim 2 , wherein the mole ratio of silica to alumina is from about 25 to about 40 and the atomic ratio of copper to aluminum is from about 0.30 to about 0.50.8. The catalyst of claim 2 , wherein the mole ratio of silica to alumina is about 30 and the atomic ratio of copper to alumina is about 0.40.9. The catalyst of claim 2 , wherein the catalyst contains ion-exchanged copper and non-exchanged copper.10. The catalyst of claim 9 , wherein the NOconversion performance of the catalyst at about 200° C. after aging is at least 90% of the NOconversion performance of the catalyst at about 200° C. prior to aging.11. The catalyst of ...

DISORDERED MOLECULAR SIEVE SUPPORTS FOR THE SELECTIVE CATALYTIC REDUCTION OF NOx

A catalyst for selective catalytic reduction of NOhaving one or more transition metals selected from Cr, Mn, Fe, Co, Ce, Ni, Cu, Zn, Ga, Mo, Ru, Rh, Pd, Ag, In, Sn, Re, Ir, Pt, and mixtures thereof supported on a support, wherein the support has a molecular sieve having at least one intergrowth phase having at least two different small-pore, three-dimensional framework structures. 1. A catalyst for selective catalytic reduction of NOcomprising:a. one or more transition metals selected from the group consisting of Cr, Mn, Fe, Co, Ce, Ni, Cu, Zn, Ga, Mo, Ru, Rh, Pd, Ag, In, Sn, Re, Ir, Pt, and mixtures thereof, andb. a support comprising an aluminosilicate, a silico-aluminophosphate, or aluminosilicate/silico-aluminophosphate molecular sieve having an intergrowth phase comprising an AEI framework,wherein the one or more transition metals are disposed inside the pores of the molecular sieve, on the external surface of the molecular sieve, or both inside the pores and on the external surface of the molecular sieve, andwherein said transition metal is present in an amount of about 0.01 to about 6 weight percent, based on the total weight of the molecular sieve.2. The catalyst of claim 1 , wherein the AEI framework structure is present in a ratio of about 1:99 to 99:1 with respect to other frameworks in the molecular sieve.3. The catalyst of claim 1 , wherein the AEI framework structure is present in a ratio of about 5:95 to about 15:85 with respect to other frameworks in the molecular sieve.4. The catalyst of claim 1 , wherein the molecular sieve is an aluminosilicate.5. The catalyst of claim 1 , wherein the molecular sieve is a silico-aluminophosphates.6. The catalyst of claim 1 , wherein said transition metal is selected from the group consisting of Cu claim 1 , Fe claim 1 , Co claim 1 , Pt claim 1 , and Mn.7. The catalyst of claim 1 , wherein said transition metal is Cu.8. The catalyst of claim 1 , wherein said transition metal is present in an amount of about 1 to ...

Hydrothermal performance of catalyst supports

A high surface area catalyst with a mesoporous support structure and a thin conformal coating over the surface of the support structure. The high surface area catalyst support is adapted for carrying out a reaction in a reaction environment where the thin conformal coating protects the support structure within the reaction environment. In various embodiments, the support structure is a mesoporous silica catalytic support and the thin conformal coating comprises a layer of metal oxide resistant to the reaction environment which may be a hydrothermal environment.

ZEOLITIC MATERIAL UZM-63

The subject invention is a novel UZM-63 material which comprises globular aggregates of crystallites having a DDR framework type with a mesopore volume of at least 0.025 cc/g, the nanocrystals having an average diameter of less than 60 nm. The novel UZM-63 material is useful for hydrocarbon conversion processes as well as separation applications, particularly the separation of olefins from paraffins. 1. A UZM-63 material comprising globular aggregates of crystallites having a DDR framework type comprising 8-ring channels , a mesopore volume of at least 0.025 cc/g , an average crystallite diameter of 60 nm or less , and a Si/Alratio from about 20 to about 50.2. The UZM-63 material of wherein the mesopore volume is at least 0.04 cc/g.3. The UZM-63 material of wherein the average crystallite diameter is about 50 nm or less.4. The UZM-63 material of wherein the average crystallite diameter is about 40 nm or less.5. (canceled)7. The method of wherein sources of aluminum are selected from the group consisting of aluminum alkoxides claim 6 , precipitated aluminas claim 6 , aluminum metal claim 6 , aluminum hydroxide claim 6 , aluminum salts and alumina sols.8. The method of wherein sources of silica are selected from the group consisting of tetraethylorthosilicate claim 6 , colloidal silica claim 6 , and precipitated silica.9. The method of wherein sources of the M metals are selected from the group consisting of halide salts claim 6 , nitrate salts claim 6 , acetate salts claim 6 , sulfate salts claim 6 , and the hydroxides of the respective alkali and alkaline earth metals.10. The method of wherein Q is an organoammonium cation represented as NR.11. The method of wherein the R groups are claim 10 , independently claim 10 , aliphatic carbon chains of the formula CH claim 10 , where n is a whole number ranging from 1 to 4 claim 10 , inclusive.12. The method of where Q is dimethyldiisopropylammonium.13. A process of separating mixtures of molecular species claim 10 , ...

Addition of a Base to Enhance Product Yield in Alkylation Reactions

A process for making styrene including providing toluene, a co-feed, and a C 1 source to a reactor containing a catalyst having acid sites and reacting toluene with the C 1 source in the presence of the catalyst and the co-feed to form a product stream containing ethylbenzene and styrene, wherein the C 1 source is selected from methanol, formaldehyde, formalin, trioxane, methylformcel, paraformaldehyde, methylal, dimethyl ether, and wherein the co-feed removes at least a portion of the acid sites on the catalyst. The co-feed can be selected from the group of aniline, amines, cresol, anisol, and combinations thereof.

Hydroisomerization and cracking catalyst for preparing biological aviation kerosene from castor oil

The present invention relates to a hydroisomerization and cracking catalyst for preparing biological aviation kerosene from castor oil as well as a preparation method and an application thereof. The catalyst takes a Al-modified titanium silicate molecular sieve (TS-1) as a carrier, and takes Ni x W and Ni x Mo as active components, wherein x is the atomic ratio of Ni to W or Ni to Mo, and x=5-10, wherein the mass of the active components accounts for 5-30% of the total mass of the catalyst; the molar ratio of Si:Ti in the Al-modified titanium silicate molecular sieve is 50-100, and the molar ratio of Si:Al is 50-100.

Selective Catalytic Reduction Catalyst System

Described are SCR catalyst systems comprising a first SCR catalyst composition and a second SCR catalyst composition arranged in the system, the first SCR catalyst composition having a faster DeNOx response time when exposed to ammonia than the second catalyst composition and the second SCR catalyst composition has a higher steady state DeNOx performance than the first catalyst composition. The SCR catalyst systems are useful in methods and systems to catalyze the reduction of nitrogen oxides in the presence of a reductant.

METHOD OF PREPARING AN STT-TYPE ZEOLITE FOR USE AS A CATALYST IN SELECTIVE CATALYTIC REDUCTION REACTIONS

A method of preparing a crystalline STT-type zeolite that has a mole ratio greater than about 15:1 of a tetravalent element oxide to a trivalent element oxide is disclosed along with a gas treatment system that incorporates the STT-type zeolite and a process for treating a gas using the STT-type zeolite. The method generally comprises forming an aqueous mixture comprising a tetravalent element oxide source, a trivalent element oxide source, a source of alkali metal, and an organic structure directing agent; maintaining the mixture under conditions that crystallize crystals of a STT-type zeolite; and recovering the crystals The STT-type zeolite crystals exhibit x-ray diffraction 2-theta degree peaks at: 8.26, 8.58, 9.28, 9.54, 10.58, 14.52, 15.60, 16.43, 17.13, 17.74, 18.08, 18.46, 19.01, 19.70, 20.12, 20.38, 20.68, 21.10, 21.56, 22.20, 22.50, 22.78, 23.36, 23.76, 23.99, 24.54, 24.92, 25.16, 25.58, 25.80, 26.12, 26.94, 27.38, 27.92, 28.30, 28.60, 29.24, 29.48, 30.08, 30.64, 31.20, 31.46, 31.80, 32.02, 32.60, 33.60, and 34.43. 1. A method for preparing a crystalline STT-type zeolite , having a mole ratio greater than about 15:1 of an oxide of a tetravalent element to an oxide of a trivalent element , said method comprising:forming an aqueous reaction mixture comprising a source of the oxide of tetravalent element; a source of the oxide of the trivalent element; a source of alkali metal; an organic structure directing agent comprising N,N,N-trimethyl-1-adamantamonium hydroxide;maintaining the aqueous reaction mixture under crystallization conditions sufficient to crystallize crystals of a STT-type zeolite having an x-ray diffraction pattern with 2 theta peaks at: 8.26, 8.58, 9.28, 9.54, 10.58, 14.52, 15.60, 16.43, 17.13, 17.74, 18.08, 18.46, 19.01, 19.70, 20.12, 20.38, 20.68, 21.10, 21.56, 22.20, 22.50, 22.78, 23.36, 23.76, 23.99, 24.54, 24.92, 25.16, 25.58, 25.80, 26.12, 26.94, 27.38, 27.92, 28.30, 28.60, 29.24, 29.48, 30.08, 30.64, 31.20, 31.46, 31.80, 32.02, 32.60, ...

ZEOLITIC CATALYTIC CONVERSION OF ALCOHOLS TO HYDROCARBONS

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

NANO-SIZED ZEOLITE SUPPORTED CATALYSTS AND METHODS FOR THEIR PRODUCTION

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

PHOTOCATALYTIC CONCRETE MATERIAL SPRAYED WITH TITANIUM DIOXIDE/ACTIVATED ZEOLITE COMPOSITE MATERIAL AND PREPARATION METHOD THEREOF

The present invention provides a photocatalytic concrete material sprayed with titanium dioxide/activated zeolite composite material and preparation method thereof, and the photocatalytic concrete material sprayed with titanium dioxide/activated zeolite composite material comprises following raw materials in parts by weight titanium dioxide 0.1-20 parts, activated zeolite molecular sieve 0.1-20 parts, dispersant 0.1-5 parts, emulsifier 0.05-2 parts, coupling agent 0.05-2 parts, cement 40-90 parts, fine sand 40-90 parts and water. In the present invention, the activated zeolite molecular sieve can load titanium dioxide photocatalytic material as a carrier, and can easily adsorb gaseous pollutant of automobile exhaust with huge specific surface area (280.1 m/g), thereby increasing photocatalytic degradation efficiency and the efficiency can reach 92%, besides, the present invention has advantages of simple preparation technology, cheap raw materials and low preparation cost, so the present invention is suitable for industrial production. 1. A photocatalytic concrete material sprayed with titanium dioxide/activated zeolite composite material , characterized in that the photocatalytic concrete material comprises following raw materials in parts by weight: titanium dioxide 0.1-20 parts , zeolite molecular sieve 0.1-20 parts , dispersant 0.1-5 parts , emulsifier 0.05-2 parts , coupling agent 0.05-2 parts , cement 40-90 parts , fine sand 40-90 parts and water.2. The photocatalytic concrete material sprayed with titanium dioxide/activated zeolite composite material of claim 1 , characterized in that the photocatalytic concrete material comprises following raw materials in parts by weight: titanium dioxide 0.5-15 parts claim 1 , zeolite molecular sieve 0.5-15 parts claim 1 , dispersant 0.1-5 parts claim 1 , emulsifier 0.05-1 parts claim 1 , coupling agent 0.05-1 parts claim 1 , cement 40-90 parts claim 1 , fine sand 40-90 parts and water.3. The photocatalytic concrete ...

PLATINUM ENCAPSULATED ZEOLITE HYDROCRACKING CATALYST AND METHODS OF MAKING SAME

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

Fcc catalyst with more than one silica, its preparation and use

Process for the preparation of a catalyst and a catalyst comprising the use of more than one silica source is provided herein. Thus, in one embodiment, the invention provides a particulate FCC catalyst comprising about 5 to about 60 wt % one or more zeolites, about 15 to about 35 wt % quasicrystalline boehmite (QCB), about 0 to about 35 wt % microcrystalline boehmite (MCB), greater than about 0 to about 15 wt % silica from sodium stabilized basic colloidal silica, greater than about 0 to about 30 wt % silica from acidic colloidal silica or polysilicic acid, and the balance clay and the process for making the same. This process results in attrition resistant catalysts with a good accessibility.

Catalyst for pyrolysis of feedstock

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

TRANSITION METAL-CONTAINING ALUMINOSILICATE ZEOLITE

A synthetic aluminosilicate zeolite catalyst containing at least one catalytically active transition metal selected from the group consisting of Cu, Fe, Hf, La, Au, In, V, lanthanides and Group VIII transition metals, which aluminosilicate zeolite is a small pore aluminosilicate zeolite having a maximum ring size of eight tetrahedral atoms, wherein the mean crystallite size of the aluminosilicate zeolite determined by scanning electron microscope is >0.50 micrometer. 1. A catalyst comprising at least one of catalytically active metal selected from copper (Cu) , iron (Fe) , or vanadium (V) on an aluminosilicate zeolite having a CHA framework and a mean crystallite size , determined by scanning electron microscope , of >0.50 microns.2. The catalyst of claim 1 , wherein the mean crystallite size determined by scanning electron microscope is >1.00 microns.3. The catalyst of claim 1 , wherein the catalytically active metal is copper.4. The catalyst of claim 3 , wherein a majority of the copper is present as copper oxide.5. The catalyst of claim 1 , wherein the catalytically active metal is iron.6. The catalyst of claim 1 , wherein the catalytically active metal is vanadium.7. The catalyst of claim 1 , wherein the catalytically active metal is present from about 0.1 to 10 weight percent based on the total weight of the zeolite.8. The catalyst of claim 1 , wherein the catalytically active metal is present from about 0.5 to 5 weight percent based on the total weight of the zeolite.9. The catalyst of claim 1 , wherein the zeolite has a silica-to-alumina ratio (SAR) of 10 to 28.10. The catalyst of claim 1 , wherein said catalyst is characterized as achieving a greater than 60% NOx conversion at temperature below 200 deg. C. after the catalyst has been hydrothermally aged at a temperature of at least 750 deg. C. for at least 24 hours in at least 10% water vapor.11. An exhaust system for an engine claim 1 , which system comprising a catalyst according to and a reductant ...

METHOD FOR STARTING UP A FLUIDIZED CATALYTIC REACTION APPARATUS USED FOR PRODUCING LOWER OLEFINS

Disclosed is a method for starting up fluidized reaction apparatus that is used for producing lower olefins from methanol or/and dimethyl ether. Said method includes after heating the catalyst bed of circulating fluidized catalytic reaction apparatus to above 200° C. or 300° C. by using a starting-up auxiliary heat source, feeding methanol or dimethyl ether raw materials to a reactor, whereby heat released by the reaction makes the temperature of the reaction system apparatus increase quickly to a designed temperature, consequently making the system reach normal operation state rapidly. Said method is suitable for starting up an exothermic fluidized catalytic reaction apparatus and can simplify the apparatus and operation, accordingly lowering the cost. 1. A method for starting up a fluidized catalytic reaction apparatus for producing lower olefins ,wherein said fluidized catalytic reaction apparatus is a circulating fluidized catalytic reaction apparatus comprising a reactor and a regenerator;wherein the reactor is a dense phase fluidized bed reactor in which is provided with a reactor heat extractor and cyclones, and the regenerator is a dense phase fluidized bed regenerator in which is provided with a regenerator heat extractor and cyclones;{'sup': '3', 'wherein the dense phase fluidized bed reactor is operated under a gauge reaction pressure of 0.05 to 0.3 MPa, a reaction temperature of 420 to 550° C., a dense phase apparent linear speed of 0.3 to 1.5 m/s and a bed layer density of 150 to 600 Kg/m;'}{'sup': '3', 'the dense phase fluidized bed regenerator is operated under a gauge reaction pressure of 0.05 to 0.3 MPa, a reaction temperature of 600 to 750° C., a dense phase apparent linear speed of 0.3 to 1.5 m/s and abed layer density of 150 to 600 Kg/m;'}in the reactor heat extractor, cooling water is used as cooling medium, wherein the cooling water is evaporated into steam by absorbing reaction heat, and the reactor heat extractor is a coil heat extractor, U ...

Process for the Selective Production of N-Methyl-2-Pyrrolidone (NMP)

This invention relates to an improved process for the selective production of N-methyl pyrrolidone (NMP) from gamma-butyrolactone and monomethyl amine preferably in aqueous form in the presence of a catalyst under comparatively milder conditions than the processes well known in the prior art of literature. The process is economically viable as it provides higher yield and selectivity for NMP which reduces the cost of separation of NMP from GBL. The catalyst shows good recyclability without significant loss in catalytic activity and no frequent regeneration is required. 110.-. (canceled)11. A process for the selective production of N-methyl-2-pyrrolidone (NMP) comprising:{'sub': 2', '2', '3, 'sup': '2', 'a) reacting feedstock monomethyl amine (MMA) and gamma-butyrolactone (GBL) in a single step in a continuously stirred tank reactor (CSTR) at a molar ratio of MMA to GBL in the range of 1 to 2, in the presence of catalyst consisting of a bronsted acidic support which is a class of zeolitic material with Si0to Al0molar ratio of 70 to 100 having specific surface area of 400 to 500 m/g and modified by oxide of one or metals selected from Al, Zr, W to the percentage of metal loading of 1 to 30 parts by weight of the support with catalyst content between 1 to 10% of total feedstock, at operating condition of temperature 130 to 250° C. and pressure 5 to 70 at 500 to 1000 agitator speed, for a period of 30 to 180 minutes to obtain a reaction mixture;'}b) cooling the reaction mixture to a temperature in the range of 20 to 25° C.;c) separating the catalyst from the reaction mixture of step b) by known methods;d) separating the product from reaction mixture of step c) by evaporation or distillation to obtain NMP at selectivity to ≥99% at a conversion of GBL to ≥98%; ande) recycling the catalyst to reactor after repeating the steps a) to d) several times.12. The process of claim 11 , wherein said MMA is in aqueous form.13. The process of claim 12 , wherein said MMA is in ...

CONDENSATION CATALYST SYSTEMS AND METHODS

A reactor system may comprise a housing; and a condensation catalyst layer within the housing comprising a condensation catalyst comprised of at least one of a base-substituted zeolite, a stannous salt, or a phosphonitrile chloride. The condensation catalyst layer may be configured to catalyze a condensation reaction of a plurality of silane diols in water flowing through the housing into a plurality of siloxanes. 1. A method , comprising:causing water and a plurality of silane diols to contact a condensation catalyst comprised in a reactor system, wherein the condensation catalyst comprises a phosphonitrile chloride; andreacting the plurality of silane diols with the condensation catalyst to form a plurality of siloxanes.2. The method of claim 1 , wherein the condensation catalyst further comprises a binder.3. The method of claim 2 , wherein the binder comprises kaolin and carboxymethylcellulose.4. The method of claim 1 , further comprising:condensing the water and a first plurality of siloxanes out of air onto a surface comprising a hydrophilic coating prior to the causing the water and the plurality of silane diols to contact the condensation catalyst; andforming the plurality of silane diols via a reaction between the hydrophilic coating and the first plurality of siloxanes.5. The method of claim 4 , further comprising at least one of removing or exchanging ions comprised in the water by contacting the water with an ion exchange resin layer in a fluid treatment system which comprises the reactor system.6. The method of claim 4 , further comprising capturing the plurality of siloxanes by causing the water to contact at least one of an activated carbon or a synthetic carbon downstream of the condensation catalyst.7. The method of claim 1 , wherein the condensation catalyst is pelletized.8. The method of claim 1 , wherein the plurality of silane diols is a plurality of dimethylsilanediol molecules.9. A fluid treatment system claim 1 , comprising:an air conditioner ...

CATALYST FOR PRODUCING HIGHER SILANE AND PROCESS FOR PRODUCING HIGHER SILANE

Provided are a catalyst for producing a higher silane with high yield at low cost by performing a reaction at relatively low temperature while inhibiting decomposition into solid silicon; and a process using the catalyst for producing a higher silane. The catalyst for producing a higher silane includes a porous oxide and is used to convert a lower silane to a higher silane wherein the porous oxide has at least regularly arranged pores and is primarily composed of silicon oxide, wherein a content of alkali metals and alkali earth metals in the porous oxide is not less than 0.00 wt % and not more than 2.00 wt %. 1. A catalyst for producing a higher silane which comprises a porous oxide and which by being contacted with a lower silane converts the lower silane to the higher silane having more silicon than the lower silane , wherein the porous oxide has at least regularly arranged pores and is primarily composed of silicon oxide , wherein a content of alkali metals and alkali earth metals in the porous oxide is not less than 0.00 wt % and not more than 2.00 wt %.2. The catalyst for producing a higher silane according to claim 1 , wherein the porous oxide has a pore diameter of not less than 0.4 nm and not more than 0.6 nm.3. The catalyst for producing a higher silane according to claim 1 , wherein the pore of the porous oxide is formed from an 8 to 12-membered oxygen ring.4. The catalyst for producing a higher silane according to claim 1 , wherein the porous oxide has a crystalline zeolite structure formed from aluminosilicate or metallosilicate.5. The catalyst for producing a higher silane according to claim 4 , wherein the crystalline zeolite structure is at least any one of BEA-type claim 4 , FER-type claim 4 , LTA-type claim 4 , MFI-type claim 4 , MOR-type and MWW-type.6. The catalyst for producing a higher silane according to claim 4 , wherein alkali metal ions or alkali earth metal ions compensating for a negative charge of the aluminosilicate or metallosilicate ...

Catalysts for Producing Paraxylene by Methylation of Benzene and/or Toluene

Embodiments disclosed herein include a process for producing paraxylene and catalyst for use in processes for producing paraxylene. In an embodiment, the process includes contacting an aromatic hydrocarbon feed comprising benzene and/or toluene with an alkylating reagent comprising methanol and/or dimethyl ether in at least one alkylation reaction zone in the presence of an alkylation catalyst comprising a molecular sieve having a Constrain Index less than 5 and under alkylation conditions. The alkylation catalyst comprises at least one of a rare earth metal or alkaline earth metal and a binder, and a majority of the at least one rare earth metal or alkaline earth metal is deposited on the molecular sieve. In addition, the process includes producing an alkylated aromatic product comprising xylenes. 1. A process for producing paraxylene , the process comprising:(a) contacting an aromatic hydrocarbon feed comprising benzene and/or toluene with an alkylating reagent comprising methanol and/or dimethyl ether in at least one alkylation reaction zone in the presence of an alkylation catalyst comprising a molecular sieve having a Constrain Index less than 5 and under alkylation conditions, wherein the alkylation catalyst comprises at least one of a rare earth metal or alkaline earth metal and a binder, and wherein a majority of the at least one rare earth metal or alkaline earth metal is deposited on the molecular sieve; and(b) producing an alkylated aromatic product comprising xylenes.2. The process of claim 1 , wherein at least 70% of the at least one rare earth metal or alkaline earth metal is deposited on the molecular sieve.3. The process of claim 2 , wherein at least 90% of the at least one rare earth metal or alkaline earth metal is deposited on the molecular sieve.4. The process of claim 1 , wherein the at least one rare earth metal or alkaline earth metal comprises at least one of lanthanum or strontium.5. The process of claim 4 , wherein the at least one rare ...

Catalyst for pyrolysis of feedstock

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

Catalyst composite for the reduction of olefins in the fcc naphtha stream

The present disclosure relates to a catalyst composition comprising (a) at least one rare earth metal, (b) at least one zeolite, and (c) at least one diluent, wherein, said rare earth metal is impregnated in at least one of (b) and (c); the ratio of said zeolite to said diluent ranges from 1:9 to 9:1; and the amount of said rare earth metal is in the range of 0.1 to 20 w/w %. The present disclosure also relates to a process for preparing a catalyst composition. Further, the present disclosure relates to a process for reducing the olefin content in a hydrocarbon stream using the catalyst of the present disclosure.

Method for preparation of modified catalysts with high catalytic performance and low coking rate

A method of manufacturing a modified zeolite catalyst may include reacting a zeolite with a metal salt to form a zeolite/metal salt complex. The zeolite may be a ZSM-5 or ZSM-11. The method may include heating the zeolite/metal salt complex to form an intermediate modified zeolite, and reacting the intermediate modified zeolite with an acid. The method may include ion exchanging the intermediate modified zeolite following the reaction with the acid to form a modified zeolite catalyst.

ZEOLITE BASED CATALYST COMPOSITION FOR THE REDUCTION OF OLEFINS IN FCC NAPHTHA

The present disclosure relates to a zeolite based catalyst composition comprising i. at least one rare earth metal, ii. at least one zeolite, and iii. optionally, at least one promoter; wherein, said rare earth metal is impregnated in said zeolite. The amount of said rare earth metal in said composition is in the range of 0.1 to 20 w/w %. The present disclosure also relates to a process for preparing a catalyst composition. Further, the present disclosure relates to a process for reducing olefin content in a hydrocarbon stream using the catalyst of the present disclosure. 1. A zeolite based catalyst composition comprising:a. at least one rare earth metal; andb. at least one zeolite,wherein, the amount of said rare earth metal is in the range of 0.1 to 20 w/w %.2. The catalyst composition as claimed in claim 1 , wherein said rare earth metal is impregnated in said zeolite.3. The catalyst composition as claimed in claim 1 , wherein the ratio of SiOto AlOin said zeolite ranges from 1:20 to 1:450.4. The catalyst composition as claimed in claim 1 , wherein the rare earth metal is selected from the group consisting of scandium claim 1 , yttrium claim 1 , lanthanum claim 1 , praseodymium claim 1 , neodymium claim 1 , promethium claim 1 , samarium claim 1 , europium claim 1 , gadolinium claim 1 , terbium claim 1 , dysprosium claim 1 , holmium claim 1 , erbium claim 1 , thulium claim 1 , ytterbium and lutetium and said metal is in a salt form selected from the group consisting of chloride claim 1 , bromide claim 1 , fluoride claim 1 , iodide claim 1 , sulfates claim 1 , phosphates claim 1 , phosphonates claim 1 , nitrates claim 1 , nitrites claim 1 , carbonates claim 1 , acetates claim 1 , bicarbonates claim 1 , hydroxides and oxides.5. The catalyst composition as claimed in claim 1 , wherein the zeolite is selected from the group consisting of ZSM-5 claim 1 , ZSM-11 claim 1 , ZSM-12 claim 1 , ZSM-22 claim 1 , ZSM-23 claim 1 , ZSM-48 claim 1 , ZSM-57 claim 1 , SAPO-5 claim 1 ...

Honeycomb structure

A honeycomb structure has grooves dented inwardly from the surfaces of the partition walls along a cell direction An open width of an open end of the groove is 0.015-0.505 mm and smaller than the open width a length of one side of each of the cells with the grooves, a bottom width of a bottom of the groove is 0.01-0.5 mm and smaller than the open width, a height from the bottom of the groove to the open end is 0.01-0.05 mm, a thickness of the partition wall in a groove portion is 50 μm or more, a ratio of the number of the cells with the grooves to the number of the total cells is 80% or more, and a value obtained by subtracting the open frontal area when the grooves excluded from the open frontal area when the grooves included is 0.1-8.0%.

Exhaust purification filter

Provided is a GPF capable of exhibiting better than conventional three-way purification function. A gasoline particulate filter (GPF) that is provided in an exhaust pipe of an engine and that performs purification by capturing particulate matter (PM) in exhaust gas is provided with a filter substrate in which a plurality of cells extending from an exhaust gas inflow-side end face to an outflow-side end face are defined by porous partition walls and in which openings at the inflow-side end face and openings at the outflow-side end face of the cells are alternately sealed; and a three-way catalyst (TWC) supported by the partition wall. The three-way catalyst is the GPF comprising a catalytic metal containing at least Rh, and a composite oxide having an oxygen storage capacity and containing Nd and Pr in a crystal structure.

METHOD FOR PRODUCING METAL EXCHANGED MICROPOROUS MATERIALS BY SOLID-STATE ION EXCHANGE

A method is disclosed for the preparation of a metal exchanged microporous materials, e.g. metal exchanged silicoaluminophosphates or metal exchanged zeolites, or mixtures of metal exchanged microporous materials, comprising the steps of providing a dry mixture of a) one or more microporous materials that exhibit ion exchange capacity and b) one or more metal compounds; heating the mixture in a gaseous atmosphere containing ammonia and one or more oxides of nitrogen to a temperature and for a time sufficient to initiate and perform a solid state ion exchange of ions of the metal compound and ions of the microporous material; and obtaining the metal-exchanged microporous material. 1. Method for the preparation of a metal exchanged crystalline microporous material or mixtures of metal exchanged crystalline microporous materials comprising the steps of providing a dry mixture containing a) one or more crystalline microporous materials that exhibit ion exchange capacity and b) one or more metal compounds; heating the mixture in a gaseous atmosphere containing ammonia and one or more oxides of nitrogen to a temperature and for a time sufficient to initiate and perform a solid state ion exchange of ions of the metal compound and ions of the crystalline microporous material; and obtaining the crystalline metal-exchanged microporous material.2. Method according to claim 1 , wherein the crystalline microporous material is selected from the group consisting of zeolite or zeotype materials.3. Method according to claim 2 , where the zeolite or zeotype materials have the framework code of AEI claim 2 , AFX claim 2 , CHA claim 2 , KFI claim 2 , LTA claim 2 , IMF claim 2 , ITH claim 2 , MEL claim 2 , MFI claim 2 , SZR claim 2 , TUN claim 2 , *BEA claim 2 , BEC claim 2 , FAU claim 2 , FER claim 2 , MOR claim 2 , LEV.4. Method according to claim 2 , wherein the zeolite or zeotype materials are selected from the group consisting of ZSM-5 claim 2 , zeolite Y claim 2 , beta zeolite ...

TRANSITION METAL/ZEOLITE SCR CATALYSTS

A method of converting nitrogen oxides in a gas to nitrogen by contacting the nitrogen oxides with a nitrogenous reducing agent in the presence of a zeolite catalyst containing at least one transition metal, wherein the zeolite is a small pore zeolite containing a maximum ring size of eight tetrahedral atoms, wherein the at least one transition metal is selected from the group consisting of Cr, Mn, Fe, Co, Ce, Ni, Cu, Zn, Ga, Mo, Ru, Rh, Pd, Ag, In, Sn, Re, Ir and Pt. 1. A catalyst composition for treating exhaust gas comprising an aluminosilicate molecular sieve having a silica-to-alumina ratio of about 8 to about 150 , having a framework selected from AEI , CHA , and AFX , and containing from 0.1 to 10 wt % of a mixture of Cu and Fe , based on the total weight of the molecular sieve , wherein the catalyst is effective to promote the reaction of NHwith NOto form nitrogen and water , selectively.2. The catalyst composition of claim 1 , wherein said framework is AEI.3. The catalyst composition of claim 1 , wherein said framework is CHA.4. The catalyst composition of claim 1 , wherein said framework is AFX.5. The catalyst composition of claim 1 , further comprising at least one binder selected from alumina claim 1 , silica claim 1 , non-zeolite silica-alumina claim 1 , natural clay claim 1 , TiO claim 1 , ZrO claim 1 , and SnO.6. The catalyst composition of claim 1 , wherein said catalyst composition contains from 0.5 to 5 wt % of said mixture of Cu and Fe.7. The catalyst composition of claim 6 , wherein said catalyst is a washcoat coated on a substrate selected from a metal flow-through substrate claim 6 , a ceramic flow-through substrate claim 6 , a wall-flow filter claim 6 , a sintered metal filter claim 6 , and a partial filter.8. A catalyst composition for treating exhaust gas comprising:a. a first aluminosilicate molecular sieve having a silica-to-alumina ratio of about 8 to about 150, having a first framework selected from AEI, CHA, and AFX, and containing from ...

COPPER CHA ZEOLITE CATALYSTS

Zeolite catalysts and systems and methods for preparing and using zeolite catalysts having the CHA crystal structure are disclosed. The catalysts can be used to remove nitrogen oxides from a gaseous medium across a broad temperature range and exhibit hydrothermal stable at high reaction temperatures. The zeolite catalysts include a zeolite carrier having a silica to alumina ratio from about 15:1 to about 256:1 and a copper to alumina ratio from about 0.25:1 to about 1:1. 1. A catalyst article comprising a honeycomb wall-flow filter substrate having an SCR catalyst composition coated on the wall flow filter comprising a CuCHA zeolite catalyst having a mole ratio of silica to alumina greater than about 15 and an atomic ratio of copper to aluminum exceeding about 0.25 , the SCR catalyst favoring reduction of nitrogen oxides and an ammonia oxidation catalyst coated on the wall flow filter , the ammonia oxidation catalyst favoring the oxidation of ammonia and comprising a CuCHA zeolite catalyst having a mole ratio of silica to alumina greater than about 15 and an atomic ratio of copper to aluminum exceeding about 0.25.2. The catalyst article of claim 1 , wherein the ammonia oxidation catalyst comprises a platinum group metal component.3. The catalyst article of claim 2 , wherein the platinum group metal component comprises Pt.4. The catalyst article of claim 3 , wherein the platinum content is between 0.02% and 1.0% by weight of the catalyst claim 3 , and the platinum loading is from about 0.5 to about 5 g/in.5. The catalyst article of claim 3 , wherein at least a portion of the wall-flow filter substrate is coated with Pt and CuCHA adapted to oxidize ammonia in the exhaust gas stream.6. The catalyst article of claim 1 , wherein the ammonia oxidation catalyst comprises SSZ-13 with at least a portion of a platinum group metal component on the washcoat.7. The catalyst article of claim 1 , wherein the wherein the wall flow filter substrate comprises a ceramic.8. The ...

High surface area pentasil zeolite and process for making same

where M is an alkali, alkaline earth, or rare earth metal such as sodium or strontium, R can be a mixture of organoammonium cations and E is a framework element such as gallium, iron, boron, or indium. These zeolites are characterized by unique x-ray diffraction patterns and compositions and have catalytic properties for carrying out various hydrocarbon conversion processes.

Modified Y-Zeolite/ZSM-5 Catalyst For Increased Propylene Production

Provided is a Fluid Catalytic Cracking catalyst composition having increased propylene production with respect to other Fluid Catalytic Cracking catalysts (measured at constant conversion). The catalyst composition comprises a particulate which comprises (a) non-rare earth metal exchanged Y-zeolite in an amount in the range of about 5 to about 50 wt %, based upon the weight of the particulate; and (b) ZSM-5 zeolite in an amount in the range of about 2 to about 50 wt %, based upon the weight of the particulate.

THERMALLY STABLE NH3-SCR CATALYST COMPOSITIONS

A catalyst composition comprising a mixture of 1. A catalyst composition comprising a mixture of{'sup': 2+', '3+', '+', '2+, '(a) a zeolite compound in an amount of 10% to 60% by weight, wherein the zeolite compound comprises cations selected from Fe, Fe, Cu, Cu or mixtures thereof,'}(b) a ceria/zirconia/alumina composite oxide, wherein the alumina content in said composite oxide is in the range of 20 to 80% by weight.2. A catalyst composition according to claim 1 , consisting of (a) and (b).3. A catalyst composition according to claim 1 , whereinthe amount of the zeolite compound in said composition is in the range from 25 to 55% by weight.4. A catalyst composition according to claim 3 , wherein the amount of the zeolite compound in said composition is in the range from 30 to 50% by weight.5. A catalyst composition according to claim 1 , wherein the ceria/zirconia/alumina composite oxide is of formula{'br': None, 'sub': 2', '3', 'x', '2', 'y', '2', 'z', 'a, '(AlO)(CeO)(ZrO)(M-oxide)'}wherein,x denotes a number from 20% to 80% by weight;y denotes a number from 5% to 40% by weight,z denotes a number from 5% to 40% by weight, anda denotes a number from 0% to 15% by weight,with the proviso that x+y+z+a=100% by weight, andM denotes a rare earth metal cation other than a Ce cation, an earth alkali metal cation, or a cation selected from a Mn, Fe, Ti, Sb or Bi cation, or M denotes individual mixtures of such cations.6. A catalyst composition according to claim 1 , wherein the amount of the cations selected from Fe claim 1 , Fe claim 1 , Cu claim 1 , Cu or mixtures thereof in the zeolite is from 0.05-15 weight % of the metal claim 1 , based on the weight of the zeolite including the cations.7. A catalyst comprising a substrate coated with a catalyst composition according to .8. A catalyst according to claim 7 , wherein the substrate is selected from the group consisting of cordierite claim 7 , mullite claim 7 , Al-Titanate claim 7 , and SiC.9. A method of using a catalyst ...

NANO-SIZED ZEOLITE SUPPORTED CATALYSTS AND METHODS FOR THEIR PRODUCTION

According to one or more embodiments described, a zeolite supported catalyst may be synthesized by a process that includes combining a colloidal mixture with a metal oxide support material to form a support precursor material, processing the support precursor material to form a support material, and impregnating the support material with one or more metals to form the zeolite supported catalyst. The colloidal mixture may include nano-sized zeolite crystals, and the nano-sized zeolite crystals may have an average size of less than 100 nm. 1. A method for synthesizing a zeolite supported catalyst , the method comprising:combining a colloidal mixture with a metal oxide support material to form a support precursor material, where the colloidal mixture comprises nano-sized zeolite crystals, and the nano-sized zeolite crystals have an average size of less than 100 nm;processing the support precursor material to form a support material; andimpregnating the support material with one or more metals to form the zeolite supported catalyst.2. The method of claim 1 , where the colloidal mixture is formed by autoclaving a mixture containing at least a quaternary ammonium salt claim 1 , silica claim 1 , alumina claim 1 , and water.3. The method of claim 2 , where the quaternary ammonium salt is tetramethylammonium hydroxide (TEAOH).4. The method of claim 2 , where the mixture containing at least quaternary ammonium salt claim 2 , silica claim 2 , aluminum claim 2 , and water has a molar ratio of:1 mole of alumina;from 15 moles to 35 moles of the quaternary ammonium salt;from 20 moles to 80 moles of silica; andfrom 250 moles to 1000 moles of water.5. The method of claim 1 , where the metal oxide support material claim 1 , which is combined with the colloidal mixture comprising nano-sized zeolites claim 1 , comprises:a small pore size metal oxide having a pore size of from 0.4 mL/g to 0.6 mL/g; anda large pore size metal oxide having a pore size of from 0.8 mL/g to 1.2 mL/g.6. The ...

Isomorphously Substituted Catalyst

Described is a selective catalytic reduction catalyst comprising a zeolitic framework material of silicon and aluminum atoms, wherein a fraction of the silicon atoms are isomorphously substituted with a tetravalent metal. The catalyst can include a promoter metal such that the catalyst effectively promotes the reaction of ammonia with nitrogen oxides to form nitrogen and HO selectively over a temperature range of 150 to 650° C. A method for selectively reducing nitrogen oxides and an exhaust gas treatment system are also described. 1. An SCR catalyst comprising a zeolitic framework material of silicon and aluminum atoms , wherein a fraction of the silicon atoms are isomorphously substituted with a tetravalent metal and the catalyst is promoted with a metal selected from Cu , Fe , Co , Ni , La , Ce , Mn , V , Ag , and combinations thereof.2. The catalyst of claim 1 , wherein the tetravalent metal comprises a tetravalent transition metal.3. The catalyst of claim 2 , wherein the tetravalent transition metal is selected from the group consisting of Ti claim 2 , Zr claim 2 , Hf claim 2 , Ge claim 2 , and combinations thereof.4. The catalyst of claim 3 , wherein the tetravalent transition metal comprises Ti.5. The catalyst of claim 1 , having a silica to alumina ratio in the range of 1 to 300.6. The catalyst of claim 5 , wherein the silica to alumina ratio is in the range of 1 to 50.7. The catalyst of claim 1 , having a tetravalent metal to alumina ratio in the range of 0.0001 to 1000.8. The catalyst of claim 7 , wherein the tetravalent metal to alumina ratio is in the range of 0.01 to 10.9. The catalyst of claim 8 , wherein the tetravalent metal to alumina ratio is in the range of 0.01 to 2.10. The catalyst of claim 1 , having a silica to tetravalent metal ratio in the range of 1 to 100.11. The catalyst of claim 10 , wherein the silica to tetravalent metal ratio is in the range of 5 to 20.12. The catalyst of claim 1 , wherein the zeolitic framework material comprises ...

METHODS FOR PRODUCING AROMATIC HYDROCARBONS FROM NATURAL GAS AND PROCESSING UNIT FOR IMPLEMENTING SAME

The invention relates to the field of gas chemistry and, more specifically, to methods and devices for producing aromatic hydrocarbons from natural gas, which involve producing synthesis gas, converting same into methanol producing, from the methanol, in the presence of a catalyst, a concentrate of aromatic hydrocarbons and water, separating the water, air stripping hydrocarbon residues from the water, and separating-out the resultant concentrate of aromatic hydrocarbons and hydrogen-containing gas, the latter being at least partially used in the production of synthesis gas to adjust the ratio therein of H:CO 1.8-2.3:1, and can be used for producing aromatic hydrocarbons. According to the invention, the production of aromatic hydrocarbons from methanol in the presence of a catalyst is carried out in two consecutively-connected reactors for synthesizing aromatic hydrocarbons: in a first, low-temperature isothermal reactor for synthesizing aromatic and aliphatic hydrocarbons, and in a second, high-temperature adiabatic reactor for synthesizing aromatic and aliphatic hydrocarbons from aliphatic hydrocarbons formed in the first reactor, and the subsequent stabilization thereof in an aromatic hydrocarbon concentrate stabilization unit. At least a portion of the hydrogen-containing gas is fed to a synthesis gas production unit and is used for producing synthesis gas using autothermal reforming technology. The installation carries out the method. The achieved technical result consists in increasing the efficiency of producing concentrates of aromatic hydrocarbons. 1. A method for producing a concentrate of aromatic hydrocarbons from natural gas , which involves producing synthesis gas , converting same into methanol , then producing , from the methanol , in the presence of a catalyst , a concentrate of aromatic hydrocarbons and water , separating the water , air stripping hydrocarbon residues from the water , and separating-out the resultant concentrate of aromatic ...

Method of Forming a Catalyst with an Ion-Modified Binder

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

Modified Crystalline Aluminosilicate for Dehydration of Alcohols

The present invention relates to a catalyst composition comprising a modified crystalline aluminosilicate of the Framework Type FER having Si/Al framework molar ratio greater than 20 characterized in that in said modified crystalline aluminosilicate the ratio between the strong acid sites and the weak acid sites, S/W, is lower than 1.0 and having the extra framework aluminum (EFAL) content lowered to less than 10 wt % preferably 5 wt % even more preferably less than 2 wt % measured by 27Al MAS NMR. The present invention further relates to a process for producing olefins from alcohols in presence of said catalyst composition. 117.-. (canceled)18. A catalyst composition , for the dehydration of alcohols in olefins having the same number of carbons , comprising a modified crystalline aluminosilicate whereinsaid modified crystalline aluminosilicate is of the Framework Type FER having Si/Al framework molar ratio greater than 20;{'sup': '27', 'in said modified crystalline aluminosilicate the extra framework aluminum, EFAL, content is lower than 15 wt % preferably 10 wt % even more preferably less than 7 wt % measured by Al MAS NMR;'}in said modified crystalline aluminosilicate the ratio between the strong acid sites and the weak acid sites, S/W, is lower than 1.0; the ratio S/W being measured by temperature-programmed desorption of ammonia and being determined by the ratio of the peak area of ammonia desorbed above 340° C. to that desorbed below 340° C.; said crystalline aluminosilicate is not steamed; and', 'said crystalline aluminosilicate is treated with an organic acidic medium and/or an organic medium; and/or', 'strong acid sites of said crystalline aluminosilicate are selectively poisoned with alkali salts or alkaline earth salts or silver so that preferably the weight percent of alkali or alkaline earth or silver on the catalyst composition is of at least 0.5% weight, more preferably at least 1% weight, most preferably at least 5% weight measured by chemical ...

INDUCTION HEATED AROMATIZATION OF HIGHER HYDROCARBONS

A reactor system for aromatization of higher hydrocarbons within a given temperature range T upon bringing a reactant stream including higher hydrocarbons into contact with a catalytic mixture. The reactor system includes a reactor unit arranged to accommodate a catalytic mixture. The catalytic mixture includes a catalyst material and a ferromagnetic material. The catalyst material is arranged to catalyze the aromatization of higher hydrocarbons. The ferromagnetic material is ferromagnetic at least at temperatures up to an upper limit of the given temperature range T, where the temperature range T is the range from between about 400° C. and about 700° C. or a subrange thereof. The reactor system also includes an induction coil arranged to be powered by a power source supplying alternating current, whereby the ferromagnetic material is heated to a temperature within the temperature range T by means of an alternating magnetic field.

EXHAUST GAS HEATING ELEMENT

An exhaust gas heating unit for an exhaust system of an internal combustion engine includes a jacket heating conductor element () including a jacket () and with an electrical heating conductor (), which extends in the jacket and is enclosed by insulating material (). A heat transfer surface formation () is arranged on, and in heat transfer contact with, an outer side of the jacket. The heat transfer surface formation includes a heat transfer element with a meandering extent along the jacket heating conductor element with a plurality of heat transfer element sections (), which pass over into one another in bent areas () and are arranged following one another in a longitudinal direction of the jacket heating conductor element. Each heat transfer element section in association with the jacket heating conductor element has a passage opening (), through which the jacket heating conductor element passes. 1. An exhaust gas heating unit for an exhaust system of an internal combustion engine , the exhaust gas heating unit comprising:a jacket heating conductor element comprising a jacket, insulating material and an electrical heating conductor extending in the jacket and enclosed by the insulating material; anda heat transfer surface formation arranged on an outer side of the jacket of the jacket heating conductor element and in heat transfer contact with the jacket of the jacket heating conductor element, the heat transfer surface formation comprising a heat transfer element with a meandering extent along the jacket heating conductor element having a plurality of heat transfer element sections, which transition from one heat transfer element section into another heat transfer element sections in bent areas and with the heat transfer element sections arranged following one another in a longitudinal direction of the jacket heating conductor element, wherein each of the heat transfer element sections has a passage opening, through which the jacket heating conductor element ...

CATALYST AND METHOD FOR PREPARATION THEREOF

A process for converting one or more C3-C12 oxygenates comprising: contacting a feed, which feed comprises one or more C3-C12 oxygenates, with hydrogen at a hydrogen partial pressure of more than 1.0 MegaPascal in the presence of a sulphided carbon-carbon coupling catalyst; wherein the carbon-carbon coupling catalyst comprises equal to or more than 60 wt % of a zeolite and in the range from equal to or more than 0.1% wt to equal to or less than 10 wt % of a hydrogenation metal, based on the total weight of the carbon-carbon coupling catalyst; and wherein the zeolite comprises 10-membered and/or 12-membered ring channels and a Silica to Alumina molar Ratio (SAR) in the range from equal to or more than 10 to equal to or less than 300. 1. A sulphided carbon-carbon coupling catalyst comprising equal to or more than 60 wt % of a zeolite and in the range from equal to or more than 0.1 wt % to equal to or less than 10 wt % of a hydrogenation metal , based on the total weight of the carbon-carbon coupling catalyst;wherein the zeolite comprises 10-membered and/or 12-membered ring channels and a Silica to Alumina molar Ratio (SAR) in the range from equal to or more than 10 to equal to or less than 300.2. The sulphided carbon-carbon coupling catalyst according to claim 1 , wherein the carbon-carbon coupling catalyst comprises in the range from equal to or more than 0.5 wt % to equal to or less than 5 wt % of a hydrogenation metal claim 1 , based on the total weight of the carbon-carbon coupling catalyst.3. The sulphided carbon-carbon coupling catalyst according to claim 1 , wherein the carbon-carbon coupling catalyst comprises one or more hydrogenation metals chosen from the group consisting of copper claim 1 , molybdenum claim 1 , tungsten claim 1 , cobalt and nickel.4. The sulphided carbon-carbon coupling catalyst according to claim 1 , wherein the carbon-carbon coupling catalyst only contains hydrogenation metals chosen from the group consisting of nickel claim 1 , cobalt ...

Intra-crystalline binary catalysts and uses thereof

The present disclosure describes, inter alia, binary catalyst compositions including a (metal) zeolite having a crystal lattice that incorporates a metal oxide, wherein the metal oxide is covalently bound to elements within the crystal lattice. The metal oxide forms an integral part of the (metal) zeolite crystal lattice, forming covalent bonds with at least the Si or Al atoms within the crystal lattice of the (metal) zeolite, and is dispersed throughout the (metal) zeolite crystal lattice. The metal oxide can substitute atoms within the crystal lattice of the (metal) zeolite.

Ammonia facilitated cation loading of zeolite catalysts

The present disclosure features a high metal cation content zeolite-based binary catalyst (e.g., a high copper and/or iron content zeolite-based binary catalyst, where the zeolite can be a chabazite) for NO x reduction, having relatively low N 2 O make, and having low corresponding metal oxide content; where the metal in the metal oxide corresponds to the metal of the metal cation. The present disclosure also describes the synthesis of the zeolite-based binary catalyst having high metal cation content.

Processes using molecular sieve ssz-27

Uses for a new crystalline molecular sieve designated SSZ-27 are disclosed. SSZ-27 is synthesized using a hexamethyl [4.3.3.0] propellane-8,11-diammonium cation as a structure directing agent.

Transition metal/zeolite scr catalysts

A method of converting nitrogen oxides in a gas to nitrogen by contacting the nitrogen oxides with a nitrogenous reducing agent in the presence of a zeolite catalyst containing at least one transition metal, wherein the zeolite is a small pore zeolite containing a maximum ring size of eight tetrahedral atoms, wherein the at least one transition metal is selected from the group consisting of Cr, Mn, Fe, Co, Ce, Ni, Cu, Zn, Ga, Mo, Ru, Rh, Pd, Ag, In, Sn, Re, Ir and Pt.

A METAL TRAP FOR USE IN FLUID CATALYTIC CRACKING (FCC)

A metal trap for an FCC catalyst include pre-formed microspheres impregnated with an organic acid salt of a rare earth element. 1. A metal trap comprising pre-formed microspheres impregnated with an organic acid salt of a rare earth element.2. The metal trap of claim 1 , wherein the pre-formed microspheres comprise kaolinite claim 1 , montmorillonite claim 1 , bentonite claim 1 , attapulgite claim 1 , kaolin claim 1 , amorphous kaolin claim 1 , metakaolin claim 1 , mullite claim 1 , spinel claim 1 , hydrous kaolin claim 1 , calcined hydrous kaolin claim 1 , clay claim 1 , or a mixture of any two or more thereof.3. (canceled)4. The metal trap of claim 1 , comprising at least 1 wt. % of the rare earth element claim 1 , on an oxide basis.5. The metal trap of claim 1 , wherein the rare earth element is lanthanum claim 1 , cerium claim 1 , ytterbium claim 1 , gadolinium claim 1 , yttrium claim 1 , neodymium claim 1 , or a mixture of any two or more thereof.6. (canceled)7. The metal trap of claim 1 , wherein the organic acid salt is a formate claim 1 , acetate claim 1 , a propionate salt claim 1 , or a mixture thereof.8. The metal trap of claim 7 , wherein the organic acid salt is a formate salt.910-. (canceled)11. The metal trap of claim 1 , wherein the pre-formed microspheres have a particle size of from about 40-150 microns.12. (canceled)13. The metal trap of claim 1 , wherein the pre-formed microspheres have a pore volume of at least about 0.10 cm/gram.14. A fluid catalytic cracking (FCC) catalyst composition comprising:a zeolite component comprising a first microsphere; anda non-zeolitic component comprising pre-formed second microspheres, separate from the first microsphere, and impregnated with an organic acid salt of a rare earth element.15. The FCC catalyst composition of claim 14 , wherein the pre-formed second microspheres comprise kaolinite claim 14 , montmorillonite claim 14 , bentonite claim 14 , attapulgite claim 14 , kaolin claim 14 , amorphous kaolin ...

DIESEL OXIDATION CATALYST

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

MOLECULAR SIEVE SSZ-111, ITS SYNTHESIS AND USE

The present disclosure is directed to a new synthetic crystalline molecular sieve material designated SSZ-111, its synthesis using N,N,N′,N′-tetramethyl-N,N′-diisobutylhexane-1,6-diammonium cations as an organic structure directing agent, and uses for SSZ-111. 2. The molecular sieve of claim 1 , and having a composition comprising the molar relationship:{'br': None, 'sub': 2', '3', '2, 'i': 'n', 'AlO:()SiO'}wherein n is in a range of 10 to 100.3. The molecular sieve of claim 1 , and having a composition comprising the molar relationship:{'br': None, 'sub': 2', '3', '2, 'i': 'n', 'AlO:()SiO'}wherein n is in a range of 15 to 50.7. A method of synthesizing the molecular sieve of claim 4 , the method comprising: (1) a source of silicon oxide;', '(2) a source of aluminum oxide;', '(3) a source of a metal (M) selected from Groups 1 and 2 of the Periodic Table;', '(4) a source of N,N,N′,N′-tetramethyl-N,N′-diisobutylhexane-1,6-diammonium cations (Q);', '(5) a source of hydroxide ions; and', '(6) water; and, '(a) preparing 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 crystallization conditions include a temperature of from 125° C. to 200° C.11. 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 an active form of the molecular sieve of . This application claims priority to U.S. Provisional Application Ser. No. 62/518,243 filed Jun. 12, 2017, which is herein incorporated by reference in its entirety.This disclosure relates to a novel synthetic crystalline molecular sieve designated SSZ-111, its synthesis, and its use in sorption and catalytic processes.Molecular sieve materials, both natural and synthetic, have been demonstrated in the past to be useful as adsorbents and ...

CATALYST WITH IMPROVED ACTIVITY/SELECTIVITY FOR LIGHT NAPHTHA AROMATIZATION

In an aspect, a method for the aromatization of hydrocarbons comprises contacting a hydrocarbon feedstream with a catalyst; wherein the catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the zeolite further comprises Na; and wherein the catalyst has an Si:Almole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5, wherein the catalyst has an aluminum content of less than or equal to 0.75 wt % excluding any binder and extrusion aide. 1. A method for the aromatization of hydrocarbons comprising:contacting a hydrocarbon feedstream with a catalyst;wherein the catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the zeolite further comprises Na; and{'sub': '2', 'wherein the catalyst has an Si:Almole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5, wherein the catalyst has an aluminum content of less than or equal to 0.75 wt % excluding any binder and extrusion aide.'}2. The method of claim 1 , wherein the hydrocarbon feedstream comprises an olefinic compound.3. The method of claim 1 , wherein the hydrocarbon feedstream comprises an alkane compound.4. The method of claim 3 , wherein the alkane compound comprises a Calkane.5. The method of claim 3 , wherein the alkane compound comprises a Calkane.6. The method of claim 5 , wherein the feed stream comprises 20 to 100 vol % of at least one of the C claim 5 , C claim 5 , or Calkane.7. The method of claim 1 , wherein the hydrocarbon feedstream comprises naphthene.8. The method of claim 1 , wherein the hydrocarbon feedstream comprises a naphtha feed.9. The method of claim 8 , wherein the naphtha feed comprises up to 1 claim 8 ,000 parts per million by weight sulfur and/or up to 100 parts per million by weight of nitrogen compounds.10. The method of claim 1 , wherein the Ge is present in an amount of ...

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

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

Zeolite catalysts having stabilized hydrogenation-dehydrogenation function

A zeolite catalyst suitable for use in shape-selective hydrocarbon conversion processes. The catalyst is modified by incorporation therein of a hydrogenation-dehydrogenation functional metal, followed by gradient selectivation with an organosilicon compound under conversion conditions, wherein the gradient selectivation conditions are characterized by a progressive temperature gradient. The use of a progressive temperature gradient during the in situ selectivation procedure unexpectedly yields a catalyst in which the hydrogenation-dehydrogenation function is stabilized, thereby enabling long duration hydrocarbon conversion processes with low by-product make.

Zeolite catalysts having stabilized hydrogenation-dehydrogenation function

A zeolite catalyst suitable for use in shape-selective hydrocarbon conversion processes. The catalyst is modified by incorporation therein of a hydrogenation-dehydrogenation functional metal, followed by gradient selectivation with an organosilicon compound under conversion conditions, wherein the gradient selectivation conditions are characterized by a progressive temperature gradient. The use of a progressive temperature gradient during the in situ selectivation procedure unexpectedly yields a catalyst in which the hydrogenation-dehydrogenation function is stabilized, thereby enabling long duration hydrocarbon conversion processes with low by-product make.

Process to prepare a catalyst for exhaust gas purification

Adsorbent comprising sepiolite and zeolite

Adsorbent comprising a sepiolite in amount of 90-10 wt.% and a zeolite in amount of 10-90 wt.% such as chabazite, mordenite, erionite, faujasite, clinoptilolite zeolites A, X, Y, omega, ZSM-5 or silicalite. The adsorbent may include a catalyst eg. a metal element, an oxide or a complex compound of at least one metal selected from the platinum group metals eg: Rh, Pd, Os, Im, Pt; the iron group metals eg: Fe, Co, Ni; group metals eg: Cu, Ag; group VII metals eg: Mn and rare earths eg: Ce, La or a combination thereof. The adsorbent is used as a deodorizer and/or to catalytically decompose the adsorbates during adsorbent regeneration.

制备和形成负载活性金属的催化剂和前体的方法

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

Catalyst and method for aromatization of c3-c4 gases, light hydrocarbon fractions and aliphatic alcohols, as well as mixtures thereof

The invention relates to hydrocarbon feedstock processing technology, in particular, to catalysts and technology for aromatization of C 3 -C 4 hydrocarbon gases, light low-octane hydrocarbon fractions and oxygen-containing compounds (C 1 -C 3 aliphatic alcohols), as well as mixtures thereof resulting in producing an aromatic hydrocarbon concentrate (AHCC). The catalyst comprises a mechanical mixture of 2 zeolites, one of which is characterized by the silica/alumina ratio SiO 2 /Al 2 O 3 =20, pre-treated with an aqueous alkali solution and modified with oxides of rare-earth elements used in the amount from 0.5 to 2.0 wt% based on the weight of the first zeolite. The second zeolite is characterized by the silica/alumina ratio SiO 2 /Al 2 O 3 =82, comprises sodium oxide residual amounts of 0.04 wt% based on the weight of the second zeolite, and is modified with magnesium oxide in the amount from 0.5 to 5.0 wt% based on the weight of the second zeolite. Furthermore, the zeolites are used in the weight ratio from 1.7:1 to 2.8:1, wherein a binder comprises at least silicon oxide and is used in the amount from 20 to 25 wt% based on the weight of the catalyst. The process is carried out using the proposed catalyst in an isothermal reactor without recirculation of gases from a separation stage, by contacting a fixed catalyst bed with a gaseous feedstock, which was evaporated and heated in a preheater. The technical result consists in achieving a higher aromatic hydrocarbon yield while ensuring almost complete conversion of the HC feedstock and oxygenates, an increased selectivity with respect to forming xylols as part of an AHCC, while simultaneously simplifying the technological setup of the process by virtue of using a reduced (inter alia, atmospheric) pressure.

Hydroprocessing scheme for production of premium isomerized light gasoline

A hydroconversion catalyst composition includes a catalytically active matrix having a surface area of between about 50 m 2 /g to about 290 m 2 /g, a silicious molecular sieve support medium distributed through the matrix and having a surface area of between about 250 m 2 /g to about 1200 m 2 /g and a catalytically active phase supported on the support medium and including a first metal selected from group IIIA of the periodic table of elements and a second metal selected from group VIB of the periodic table of elements. The matrix preferably further includes aluminum, gallium, cobalt, molybdenum, and phosphorus.

Process for producing reformulated gasoline by reducing sulfur, nitrogen and olefin

A process for upgrading a nitrogen and sulfur rich heavy naphtha feedstock includes the steps of providing a naphtha feedstock having an initial nitrogen content, an initial sulfur content and an initial octane number; contacting the naphtha feedstock with an acid source so as to provide a reduced nitrogen feedstock having a reduced nitrogen content which is less than the initial nitrogen content; contacting the reduced nitrogen feedstock with a hydroconversion catalyst system under a hydrogen atmosphere, temperature and pressure so as to provide a final product having a final nitrogen content which is less than the initial nitrogen content, a final sulfur content which is less than the initial sulfur content, and having a final octane number which is substantially equal to or greater than the initial octane number of the feedstock, and wherein the final product has an increased isomerized component and substantially no increase in aromatic content with respect to the feedstock.

A hydroconversion catalyst

A hydroconversion catalyst composition includes a catalytically active matrix having a surface area of between about 50 m<SP>2</SP>/g to about 290 m<SP>2</SP>/g, a silicious molecular sieve support medium distributed through the matrix and having a surface area of between about 250 m<SP>2</SP>/g to about 1200 m<SP>2</SP>/g and a catalytically active phase supported on the support medium and including a first metal selected from group IIIA of the periodic table of elements eg. Ga or B, a second metal selected from group VIB of the periodic table of element eg. Cr or Mo. The matrix preferably further includes aluminum, gallium, cobalt, molybdenum, and phosphorus.

Metal zeolite catalyst preparation

Zeolite-metal catalysts having a substantial amount of catalytically active metal, e.g. iron, deposited in the cavities of the zeolite in zero-valent, small cluster form, are prepared by vaporizing the metal under low vapor pressure conditions in the vicinity of an organic liquid solvent, e.g. toluene, such that the metal dissolves in the solvent as a labile solvated zero-valent metal complex. This complex is contacted with the zeolite so that the complex diffuses into the cavities of the zeolite. Upon subsequent warming the solvated metal complex decomposes, leaving zero-valent small metal clusters in the zeolite cavities.