СПОСОБ И УСТРОЙСТВО ДЛЯ УМЕНЬШЕНИЯ СОДЕРЖАНИЯ NOxИ N2O В ГАЗАХ

Изобретение относится к способу уменьшения содержания оксидов азота в газах, в частности в технологических и отходящих газах, а также к применяемому для этого устройству. Способ включает пропускание N2O- и NOx-содержащего газа через ряд двух слоев катализатора, содержащих один тип или несколько типов нагруженных железом цеолитов, добавление восстановителя для NOx между этими слоями катализатора, поддержание температуры менее чем 500°С в первом слое катализатора и во втором слое катализатора, поддержание газового давления, по меньшей мере, 2 бар в обоих слоях катализаторов, выбор такой объемной скорости в первом и втором слоях катализатора, что в первом слое катализатора происходит разложение N2O, до содержания не более чем 90% в расчете на содержание N2O на входе первого слоя катализатора и устанавливается содержание N2O более чем 200 частей на млн. и что во втором слое катализатора происходит дальнейшее разложение содержащегося в газе N2O, по меньшей мере, на 30% в расчете на содержание ...

СОДЕРЖАЩЕЕ МЕДЬ МОЛЕКУЛЯРНОЕ СИТО ИЗ ЛЕВИНА ДЛЯ СЕЛЕКТИВНОГО ВОССТАНОВЛЕНИЯ NOx

Настоящее изобретение относится к способу получения содержащего медь молекулярного сита из левина, к его применению в качестве катализатора для селективного восстановления оксидов азота NOи к способу селективного восстановления оксидов азота NOв присутствии полученного катализатора. Молекулярное сито имеет молярное отношение диоксида кремния к оксиду алюминия менее 30 и атомное отношение Cu:Al менее 0,45. Содержащее медь молекулярное сито из левина получено путем ионного обмена указанного молекулярного сита с аммиачным раствором ионов меди при температуре от около 20°С до около 35°С и рН от около 5 до около 14. Технический результат - сохранение по меньшей мере 60% площади поверхности молекулярного сита после воздействия температуры от около 750°С до около 950°С в присутствии до 10 об.% водяного пара в течение периода времени от около 1 до около 48 часов. 3 н. и 3 з.п. ф-лы, 10 ил., 4 табл., 4 пр.

КАТАЛИЗАТОРЫ ОБРАБОТКИ НЕСТАЦИОНАРНЫХ ВЫБРОСОВ NO

Изобретение относится к композиции катализатора для обработки выхлопного газа. Данная композиция включает a) первое молекулярное сито, имеющее предварительно состаренную решетку ВЕА или решетку ВЕА с изоморфным железом, в котором указанное первое молекулярное сито содержит от 0,5 до 5 весовых процентов, полученного ионным обменом или свободного железа; и b) второе молекулярное сито, имеющее кристаллическую структуру с малыми порами и содержащее от 0,5 до 5 весовых процентов полученной ионным обменом или свободной Cu. При этом отношение указанного первого молекулярного сита и указанного второго молекулярного сита составляет от 0,1 до 1. Предлагаемая композиция катализатора характеризуется более высокой общей конверсией NOпри равном или более низком проскоке NH, чем любой молекулярно-ситовой компонент, взятый отдельно. Настоящее изобретение относится также к катализатору для обработки выхлопного газа, включающему данную композицию, и способу обработки выхлопного газа. 3 н. и 11 з.п. ф-лы, ...

ДЕЗАЛЮМИНИРОВАННЫЙ ЦЕОЛИТ NU-86, СПОСОБ ЕГО ПОЛУЧЕНИЯ (ВАРИАНТЫ), КАТАЛИЗАТОР НА ЕГО ОСНОВЕ И ЕГО ИСПОЛЬЗОВАНИЕ ПРИ КОНВЕРСИИ УГЛЕВОДОРОДОВ

Изобретение относится к модифицированному цеолиту NU-86, содержащему кремний и по меньшей мере один элемент Т, выбранный из группы, состоящей из алюминия, железа, галлия и бора. Элемент Т удален из каркаса исходного неочищенного синтетического цеолита NU-86. Общее атомное соотношение Si/Т превышает примерно 20. Удаление элемента Т из цеолитного каркаса (или решетки) осуществляют посредством по меньшей мере одной термической обработки, осуществляемой, в случае необходимости, в присутствии паров воды, с последующим по меньшей мере одним кислотным травлением в по меньшей мере одном растворе минеральной или органической кислоты, или лучше посредством прямого кислотного травления. Изобретение также относится к катализатору, содержащему указанный цеолит, находящийся по меньшей мере частично в кислотной форме, и к использованию указанного катализатора при конверсии углеводородов, в частности, при олигомеризации олефинов С2-С8. Модифицированный цеолит NU-86 настоящего изобретения при введении его ...

СПОСОБ РЕГУЛИРОВКИ СОДЕРЖАНИЯ 2-ФЕНИЛЬНОГО ИЗОМЕРА ЛИНЕЙНОГО АЛКИЛБЕНЗОЛА И КАТАЛИЗАТОР, ИСПОЛЬЗУЕМЫЙ В ЭТОМ СПОСОБЕ

Изобретение относится к алкилированию арильных соединений олефинами. Способ регулировки содержания 2-фенильного изомера в линейном алкилбензоле, получаемом путем алкилирования бензола олефином, включает реакцию олефина с бензолом в технологическом потоке, содержащем воду, в присутствии катализатора, а также контроль концентрации воды в сырье в диапазоне от совершенно сухого до 100 м.д. воды. Указанный катализатор в качестве первого компонента содержит цеолит, выбранный из группы, состоящей из фожазитов, содержащих редкоземельные элементы, и их смесей, и в качестве второго компонента - цеолит, выбранный из группы, состоящей из UZM-8, цеолит MWW, цеолит ВЕА, цеолит OFF, цеолит MOR, цеолит LTL, цеолит MTW, BPH/UZM-4 и их смеси. В соответствии с изобретением можно получать линейный алкилбензол, имеющий заданное содержание 2-фенильного изомера. 7 з.п. ф-лы, 1 ил., 1 пр.

EMM-28 - новый синтетический кристаллический материал, его получение и применение

Изобретение относится к новому синтетическому кристаллическому материалу ЕММ-28, который синтезирован в присутствии органического направляющего агента (Q) для формирования структуры, выбранного из одного или более из следующих дикатионов:ЕММ-28 можно использовать в реакциях превращения органических соединений и сорбционных процессах. 14 н. и 4 з.п. ф-лы, 26 пр., 3 табл., 2 ил.

СПОСОБ КОНВЕРСИИ УГЛЕВОДОРОДОВ С ИСПОЛЬЗОВАНИЕМ СВЯЗАННОГО ЦЕОЛИТОМ ЦЕОЛИТНОГО КАТАЛИЗАТОРА

Использование: в нефтехимии. Сущность: углеводородное сырье контактирует в условиях конверсии углеводородов со связанным цеолитом цеолитным катализатором, включающим (а) первые кристаллы первого цеолита и (б) связующее вещество, содержащее вторые кристаллы второго цеолита, средний размер частиц которых меньше размера первых кристаллов, причем вторые кристаллы находятся в сращенном состоянии с первыми кристаллами и образуют на них покрытие или частичное покрытие. Технический результат - повышение селективности процесса. 50 з.п. ф-лы, 8 табл., 4 ил.

НОВАЯ МОЛЕКУЛЯРНО-СИТОВАЯ КОМПОЗИЦИЯ ЕММ-13, СПОСОБЫ ЕЕ ПОЛУЧЕНИЯ И ПРИМЕНЕНИЯ

Настоящее изобретение относится к синтезу молекулярных сит. Предложен молекулярно-ситовой материал EMM-13, имеющий каркас тетраэдрических атомов, связанных мостиками из атомов кислорода, который определяется специфическими атомными координатами элементарной ячейки в нанометрах. Материал характеризуется специфической рентгенограммой. Предложенный материал используют в качестве катализатора превращения углеводородов. Техническим результатом является получение нового материала, обладающего активностью и стабильностью в каталитических реакциях превращения углеводородов. 2 н. и 11 з.п. ф-лы, 17 ил., 8 табл., 17 пр.

КАТАЛИЗАТОР И СПОСОБ ПОЛУЧЕНИЯ УКСУСНОЙ КИСЛОТЫ И ДИМЕТИЛОВОГО ЭФИРА

Изобретение относится к способу совместного получения уксусной кислоты и диметилового эфира из смеси метанола и метилацетата с увеличением срока службы каталитической композиции. Способ включает введение во взаимодействие метанольного сырья и метилацетатного сырья с каталитической композицией в зоне реакции при температуре, равной от 200 до 260°С, с получением уксусной кислоты и диметилового эфира, и где указанная каталитическая композиция включает цеолит, который содержит 2-мерную канальную систему, содержащую по меньшей мере один канал, образованный 10-членными кольцами, и обладает молярным отношением диоксид кремния : оксид алюминия, составляющим по меньшей мере 22:1. Изобретение относится также к каталитической композиции, обладающей увеличенным сроком службы при осуществлении способа совместного получения уксусной кислоты и диметилового эфира из смеси метанола и метилацетата. 2 н. и 21 з.п. ф-лы, 4 табл., 7 пр.

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.

МОЛЕКУЛЯРНОЕ СИТО, ЕГО ПОЛУЧЕНИЕ И ПРИМЕНЕНИЕ

Группа изобретений относится к молекулярному ситу, в частности к ультрамакропористому молекулярному ситу, а также к способу получения молекулярного сита и его применению в качестве катализатора. Молекулярное сито имеет схематическую химическую композицию представленную формулой «первый оксид ⋅ второй оксид» или формулой «первый оксид ⋅ второй оксид ⋅ органический темплат ⋅ вода», в которой молярное соотношение первого оксида и второго оксида находится в диапазоне от 5 до ∞, первый оксид выбран из группы, состоящей из диоксида кремния, диоксида германия, диоксида олова, диоксида титана и диоксида циркония, предпочтительно диоксида кремния или комбинации диоксида кремния и диоксида германия, второй оксид выбран из группы, состоящей из оксида алюминия, оксида бора, оксида железа, оксида галлия, оксида редкоземельного элемента, оксида индия и оксида ванадия, предпочтительно оксида алюминия, молярное соотношение воды и первого оксида находится в диапазоне от 5 до 50, молярное соотношение темплата ...

НОВАЯ МОЛЕКУЛЯРНО-СИТОВАЯ КОМПОЗИЦИЯ ЕММ-12, СПОСОБЫ ЕЕ ПОЛУЧЕНИЯ И ПРИМЕНЕНИЯ

Настоящее изобретение относится к молекулярным ситам, их получению и использованию. Предложен материал EMM-12, имеющий структуру, охарактеризованную в формуле рентгенограммой. EMM-12 в свежеприготовленной и прокаленной формах имеет рентгенограмму, включающую пики, соответствующие дифракционным максимумам в диапазоне от 14,17 до 12,57Å, дифракционным максимумам в диапазоне от 12,1 до 12,56 Å. Материал имеет также неразрешенное рассеивание в интервале от примерно 8,85 до 11,05 Å или не содержащую максимумов область между пиками, соответствующими дифракционным максимумам в диапазоне от 10,14 до 12,0 Å и дифракционным максимумам в диапазоне от 8,66 до 10,13 Å. Согласно изобретению измеренная интенсивность, для которой сделана поправка на уровень фона, в точке с наименьшим значением составляет не менее 50% от значения интенсивности, соответствующей аналогичному межплоскостному расстоянию на линии, соединяющей максимумы в диапазоне от 10,14 до 12,0 Å и в диапазоне от 8,66 до 10,13 Å. Предложен ...

ФОСФОРСОДЕРЖАЩИЙ КАТАЛИЗАТОР ДЛЯ ПРЕВРАЩЕНИЯ ОКСИГЕНАТОВ В ОЛЕФИНЫ

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

ВЫСОКОАКТИВНЫЕ МОЛЕКУЛЯРНЫЕ СИТА СО СТРУКТУРОЙ ТИПА МТТ

Изобретение относится к области катализа. Описан способ получения молекулярного сита ZSM-23, включающий: а) приготовление смеси, способной образовать указанное молекулярное сито; причем указанная смесь включает источники щелочного или щелочноземельного металла (М), оксида трехвалентного элемента (X), оксида четырехвалентного элемента (Y), воду и направляющий структуру агент (R) формулы (CH)NCHCHCHN(CH)CHCHCHN(CH), и имеет состав, в мольных отношениях, в пределах следующих диапазонов: YO/XOот 25 до 29, HO/YOот 5 до 100, OH/YOот 0,05 до 0,5, M/YOот 0,05 до 0,5, R/YOот >0 до <0,5, и b) выдержку указанной смеси в условиях, достаточных для получения указанного ZSM-23, где указанные достаточные условия включают температуру от примерно 150 до 200°С. Описан способ депарафинизации содержащего парафины сырья путем изомеризации парафинов, в присутствии молекулярного сита ZSM-23, полученного описанным выше способом. Технический результат - увеличение каталитической активности. 2 н. и 10 з.п. ф-лы, ...

СПОСОБ ПОЛУЧЕНИЯ АЛКИЛАРОМАТИЧЕСКИХ СОЕДИНЕНИЙ С ИСПОЛЬЗОВАНИЕМ ЕММ-12

Изобретение относится к области органической химии. Способ получения моноалкилароматического соединения осуществляют контактированием сырья, содержащего алкилируемое ароматическое соединение и алкилирующий агент, в условиях каталитзируемой реакции алкилирования. Катализатор представляет собой молекулярное сито ЕММ-12. Использованное молекулярное сито в свежеприготовленной и прокаленной формах характеризуется рентгенограммой. Рентгенограмма содержит пики, соответствующие дифракционным максимумам в диапазоне от 14,17 до 12,57 Å, дифракционным максимумам в диапазоне от 12,1 до 12,56 Å, неразрешенное рассеивание в интервале от примерно 8,85 до 11,05 Å, или не содержащую максимумов область между пиками, соответствующими дифракционным максимумам в диапазоне от 10,14 до 12,0 Å и дифракционным максимумам в диапазоне от 8,66 до 10,13 Å. Измеренная интенсивность, для которой сделана поправка на уровень фона, в точке с наименьшим значением указанной области, не содержащей пиков, составляет не менее ...

Применение синтетических цеолитов для увеличения селективности при получении 4,4-диметил-1,3-диоксана (варианты)

Изобретение относится к области основного органического и нефтехимического синтеза и может быть использовано в производстве 4,4-диметил-1,3-диоксана путем конденсации трет-бутанола и формальдегида. Предложены синтетические цеолиты общей формулы Na12[(AlO2)12(SiO2)12]⋅xH2O марки NaA с диаметром пор 4 или Ca4,5Na3[(AlO2)12(SiO2)12]⋅xH2O марки СаА с диаметром пор 5 в качестве гетерогенных сокатализаторов. При этом синтез ДМД проводят в присутствии фосфорной кислоты, взятой в качестве базового кислотного катализатора. Технический результат: увеличение селективности образования 4,4-диметил-1,3-диоксана. 2 н. и 1 з.п. ф-лы, 1 табл., 3 пр.

СПОСОБЫ ПОЛУЧЕНИЯ КРИСТАЛЛИЧЕСКОГО ЦЕОЛИТА

Описан способ получения кристаллического цеолита из реакционной смеси, содержащей количество воды, достаточное только для того, чтобы, при желании, реакционной смеси можно было бы придать определенную форму. По данному способу реакционную смесь нагревают в условиях кристаллизации и в отсутствие внешней жидкой фазы, так что перед высушиванием кристаллов нет необходимости в удалении избыточной жидкости из закристаллизованного материала. Способ позволяет сократить количество воды для кристаллизации и получить формованные цеолиты без добавления связующего. 2 с. и 40 з.п.ф-лы.

ЦЕОЛИТ NU-86 И СПОСОБ ЕГО ПОЛУЧЕНИЯ

Цеолит, обозначенный как цеолит NU-86, имеющий молярный состав, выраженный формулой 100 XO2: ≅10 Y2O3: ≅20 R2/n0, где R - один или несколько катионов с валентностью n, X - кремний и/или германий, Y - один или несколько из алюминия, железа, галлия, бора, титана, ванадия, циркония, молибдена мышьяка, сурьмы, хрома и марганца, и имеющий картину дифракции рентгеновских лучей, включая линии, показанные в табл.1, причем цеолит получен из реакционной смеси, состоящей из XO2 (предпочтительно двуокись кремния), Y2O3 (предпочтительно окись алюминия) и катиона полиметилен - альфа, омега-диаммония. Этот цеолит пригоден в качестве катализатора для различных реакций. 2 с. и 6 з.п. ф-лы, 8 ил., 8 табл.

СПОСОБ ПОЛУЧЕНИЯ СИНТЕТИЧЕСКОГО КРИСТАЛЛИЧЕСКОГО АЛЮМОСИЛИКАТА

Изобретение относится к способам получения синтетических кристаллических алюмосиликатов (цеолитов), применяемых в качестве адсорбентов, катализаторов и компонентов моющих составов. Сущность изобретения: смешивают в водно-щелочной среде SiO2 и Al2O3 или их гидраты, или силикаты щелочных металлов и алюминаты щелочных металлов, минерализаторы и при необходимости затравку при следующих мольных отношенияx: SiO2 /Al2O3 = 15-40, ОН-/SiO2 = 0,1-0,2, Н2О/SiO2 = 20-60. 3 з.п. ф-лы, 4 табл., 3 ил.

СПОСОБЫ ПОЛУЧЕНИЯ НАНОЦЕОЛИТОВ И СПОСОБ ИЗВЛЕЧЕНИЯ НАНОЦЕОЛИТОВ ИЗ ВОДНОЙ СУСПЕНЗИИ

Изобретение относится к получению наноцеолитов. Предложены варианты осуществления способа извлечения наноцеолитов из водной суспензии. Способ включает воздействие центробежной силы на водную суспензию частиц наноцеолита с отделением надосадочной жидкости от твердой фазы, которая содержит наноцеолиты и остаточные примеси. Твердую фазу подвергают обработке раствором, который эффективно растворяет или превращает остаточные примеси и агломерирует наноцеолиты. Образованные агломерированные частицы наноцеолита извлекают из суспензии путем фильтрации. Изобретение обеспечивает упрощение способа выделения наночастиц цеолитов из суспензии и сокращает продолжительность процесса. 2 н. и 8 з.п. ф-лы, 1 ил., 1 пр.

СПОСОБ IN-SITU ПОЛУЧЕНИЯ КАТАЛИЗАТОРА ДЛЯ ПОЛУЧЕНИЯ ПО МЕНЬШЕЙ МЕРЕ ОДНОГО ИЗ ТОЛУОЛА, ПАРА-КСИЛОЛА И НИЗШИХ ОЛЕФИНОВ, А ТАКЖЕ ПРОЦЕСС РЕАКЦИИ

Настоящее изобретение относится к способу in-situ получения катализатора для получения по меньшей мере одного из толуола, пара-ксилола и низших олефинов, а также к процессу реакции получения по меньшей мере одного из толуола, пара-ксилола и низших олефинов, и относится к области химической технологии. Описан способ in-situ получения катализатора, в котором модификатор приводят в контакт с цеолитным молекулярным ситом в реакторе для in-situ получения катализатора для получения пара-ксилола, толуола и/или низших олефинов из сырьевого материала, содержащего метанол и/или диметиловый эфир; и реактор представляет собой реактор для получения пара-ксилола, толуола и/или низших олефинов из сырьевого материала, содержащего метанол и/или диметиловый эфир; при этом модификатор содержит по меньшей мере один из следующих модификаторов: Модификатор I: фосфорсодержащий реагент и силилирующий реагент; Модификатор II: силилирующий реагент; Модификатор III: силилирующий реагент и водяной пар; Модификатор ...

КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ И СПОСОБ ТРАНСАЛКИЛИРОВАНИЯ АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ

... 1. Каталитическая композиция, включающая цеолит и неорганическое связующее вещество, где цеолит имеет кристаллическую структуру с отверстиями, образованными 12 тетраэдрами, а связующим веществом является γ-оксид алюминия, при этом указанная композиция отличается объемом пор, получаемым при суммировании присутствующих в указанной каталитической композиции мезопористой и макропористой составляющих, превышающим или равным 0,7 см3/г, причем по меньшей мере 30% указанного объема состоит из пор, диаметр которых более 100 нм. 2. Каталитическая композиция по п.1, прочность на раздавливание которой больше или равна 1,7 кг/мм. 3. Каталитическая композиция по п.1, кажущаяся плотность которой не превышает 0,5 г/ см3. 4. Каталитическая композиция по п.1 в виде частиц, имеющих диаметр не менее 1,8 мм. 5. Каталитическая композиция по п.4 в виде частиц, имеющих диаметр не менее 2,0 мм. 6. Каталитическая композиция по п.1 в виде цилиндрических гранул. 7. Каталитическая композиция по п.1, в которой цеолит ...

КАТАЛИЗАТОР И СПОСОБ ПОЛУЧЕНИЯ УКСУСНОЙ КИСЛОТЫ И ДИМЕТИЛОВОГО ЭФИРА

... 1. Способ совместного получения уксусной кислоты и диметилового эфира из смеси метанола и метилацетата, способ включает введение во взаимодействие метанольного сырья и метилацетатного сырья с каталитической композицией в зоне реакции при температуре, равной от 200 до 260°C, с получением уксусной кислоты и диметилового эфира, и где указанная каталитическая композиция включает цеолит, который содержит 2-мерную канальную систему, содержащую по меньшей мере один канал, образованный 10-членными кольцами, и обладает молярным отношением диоксид кремнияюксид алюминия, составляющим по меньшей мере 22:1.2. Способ по п. 1, в котором цеолит дополнительно содержит по меньшей мере один канал, образованный 8-членными кольцами.3. Способ по п. 2, в котором цеолит обладает каркасной структурой, выбранной из группы, включающей FER, HEU, MFS, DAC, STI, NES, MWW и TER.4. Способ по п. 3, в котором цеолит обладает каркасной структурой FER.5. Способ по п. 4, в котором цеолитом, обладающим каркасной структурой ...

ЧЕТВЕРТИЧНЫЙ КАТИОН АММОНИЯ НА ОСНОВЕ МОРФОЛИНИЯ И ПОЛУЧЕННЫЙ С ЕГО ИСПОЛЬЗОВАНИЕМ ЦЕОЛИТ ТИПА AEI

Настоящее изобретение относится к алюмосиликатному цеолиту, способу изготовления алюмосиликатного цеолита и кристаллическому цеолиту AEI. Алюмосиликатный цеолит содержит по меньшей мере 90% чистой фазы цеолита AEI. Цеолит AEI содержит кристаллы, имеющие пластинчатую морфологию, где по меньшей мере 50% кристаллов имеют по меньшей мере одно отношение в по меньшей мере одной паре размеров в интервале от 5:1 до 20:1. По меньшей мере 50% кристаллов имеют толщину в интервале от 30 до 100 нм. Способ изготовления алюмосиликатного цеолита, имеющего каркас AEI, включает реакцию смеси, содержащей оксид кремния, фоязит, соединение четвертичного аммония, содержащее катион 2,4,4,6-тетраметилморфолиния, гидроксид щелочного металла и воду. Отношение OH/Si равно 0,4-0,8. Температура реакции по меньшей мере 100°С и в течение времени, достаточного для образования кристаллов алюмосиликатного цеолита, имеющего каркас AEI. Кристаллический цеолит AEI имеет поры, содержащие катион 2,4,4,6-тетраметилморфолиния.

СПОСОБ ПРИГОТОВЛЕНИЯ КАТАЛИЗАТОРА И СПОСОБ ПОЛУЧЕНИЯ ИЗОПРОПИЛБЕНЗОЛА С ИСПОЛЬЗОВАНИЕМ ЭТОГО КАТАЛИЗАТОРА

Изобретение относится к способу получения изопропилбензола в процессе алкилирования бензола пропиленом при температуре 170-230°C, давлении от атмосферного до 50 атм, мольном отношении бензол/пропилен в исходной смеси от 4:1 до 10:1, весовой скорости подачи исходной смеси от 0,2 до 10 ч-1с использованием катализатора на основе цеолита Бета, приготовленного контактированием цеолита Бета с раствором нитрата аммония для удаления соединений натрия и переведения цеолита в водородную форму, с последующими стадиями грануляции со связующим, сушки и прокаливания гранул, причем цеолит Бета перед грануляцией со связующим предварительно подвергают обработке раствором хелатирующего агента, а затем обрабатывают перегретым водяным паром при температуре не выше 550°С в течение не менее 2 ч, в качестве хелатирующиего агента применяют сульфосалициловую кислоту, этилендиаминтетрауксусную кислоту ЭДТА, сульфобензойную кислоту, 3-гидроксинафталин-1,4-дисульфокислоту. Технический результат заключается в увеличении ...

СПОСОБ КРЕКИНГА И УЛУЧШЕННЫЕ КАТАЛИЗАТОРЫ ДЛЯ ОСУЩЕСТВЛЕНИЯ УКАЗАННОГО СПОСОБА

... 1. Способ крекинга углеводородных смесей, отличающийся тем, что способ осуществляют в присутствии катализатора, содержащего цеолит ERS-10. ! 2. Способ по п.1, в котором катализатор содержит два различных компонента: (а) компонент, содержащий один или более катализаторов крекинга, и (b) компонент, содержащий цеолит ERS-10. ! 3. Способ по п.1, отличающийся тем, что способ представляет собой крекинг с псевдоожиженным слоем катализатора. ! 4. Способ по п.1, выполняемый в присутствии катализатора, включающего: ! a) первый компонент, содержащий один или более катализаторов, выбранных из цеолитов, аморфных катализаторов крекинга на основе неорганических оксидов и кристаллических нецеолитовых катализаторов крекинга на основе неорганических оксидов, ! b) второй компонент, содержащий цеолит ERS-10. ! 5. Способ по пп.2, 3 или 4, в котором катализатор или смесь катализаторов, содержащихся в компоненте (а), распределены в матрице из неорганического оксида. ! 6. Способ по п.4, в котором в компоненте ...

РАЗДЕЛЕНИЕ И ХРАНЕНИЕ ТЕКУЧИХ СРЕД С ИСПОЛЬЗОВАНИЕМ ITQ-55

УПРАВЛЯЕМЫЕ ЩЕЛОЧНЫЕ ОБРАБОТКИ НА МОЛЕКУЛЯРНЫХ СИТАХ

ВЫСОКОКРЕМНЕЗЕМНЫЙ ЦЕОЛИТ AEI

СПОСОБ ПОЛУЧЕНИЯ АЛКИЛАРОМАТИЧЕСКИХ СОЕДИНЕНИЙ С ИСПОЛЬЗОВАНИЕМ EMM-13

... 1. Способ получения моноалкилароматического соединения, включающий контактирование сырья, содержащего алкилируемое ароматическое соединение и алкилирующий агент, в условиях реакции алкилирования с катализатором, включающим молекулярное сито, имеющее каркасную структуру тетраэдрических атомов, связанных через атомы кислорода, причем тетраэдрический атомный каркас определяется элементарной ячейкой, имеющей атомные координаты (в нанометрах), приведенные в нижеследующей таблице: ! Атом х/а y/b z/c Uизотр.зан. Т1 0,6667 0,3333 0,1126 (2) 0,00649 1,0 Т2 0,4652 (5) 0,2326 (3) 0,1754 (3) Т3 0,3901 (5) 0,0 0,1897 (4) Т4 0,6667 0,3333 0,2403 (4) Т5 0,6667 0,3333 0,3575 (4) Т6 0,3894 (5) 0,0 0,3050 (4) Т7 0,4215 (5) 0,2108 (2) 0,3593 (3) Т8 0,2502 (5) 0,1251 (3) 0,4450 (2) Т9 0,6667 0,3333 0,0 O10 0,6667 0,3333 0,0562 (1) 0,010 1,0 O11 0,5420 (3) 0,2710 (1) 0,1282 (2) O12 0,3876 (5) 0,1037 (2) 0,1681 (4) O13 0,5408 (3) 0,2704 (2) 0,2230 (3) O14 0,6667 0,3333 0,2991 (4) O15 0,3725 (2) 0,0 0,2473 (3 ...

ОКИСЛИТЕЛЬНЫЙ КАТАЛИЗАТОР И СИСТЕМА ВЫПУСКА ВЫХЛОПНЫХ ГАЗОВ ДЛЯ ДИЗЕЛЬНОГО ДВИГАТЕЛЯ

МОДУЛИ И СПОСОБЫ ПОДГОТОВКИ ТОПЛИВА

... 1. Модуль подготовки топлива для обработки сгораемого топлива перед сжиганием, включающий:корпус, имеющий впускной и выпускной концы и определяющий сквозной канал для топлива между ними; ивставной блок подготовки топлива, расположенный в сквозном канале, таким образом, что топливо, протекающее в канале между впускным и выпускным концами корпуса, вступает в контакт с блоком подготовки топлива, причемвставной блок подготовки топлива включает:(i) массу каталитических металлических элементов, которые составляет каталитический металл;(ii) массу твердого полимерного каталитического материала в форме пластинок, диспергированных в массе каталитических металлических материалов, причем пластинки из твердого полимерного каталитического материала составляют полимерный связующий материал и каталитическую смесь твердых частиц цеолита и твердых частиц редкоземельного металла или оксида металла, смешанных в твердом полимерном связующем материале.2. Модуль подготовки топлива по п.1, дополнительно включающий ...

Материалы EMM-23, способы их получения и их применение

UZM-45 АЛЮМОСИЛИКАТНЫЙ ЦЕОЛИТ, СПОСОБ ЕГО ПОЛУЧЕНИЯ И ПРОЦЕССЫ С ЕГО ИСПОЛЬЗОВАНИЕМ

... 1. Микропористый кристаллический цеолит, имеющий трехмерный каркас, по меньшей мере, из AlOи SiOтетраэдрических звеньев и эмпирический состав «как синтезирован» в безводном состоянии, выраженный эмпирической формулой:,где М представляет собой, по меньшей мере, один обмениваемый катион, выбранный из группы, состоящей из щелочных, щелочноземельных и редкоземельных металлов, "m" представляет собой мольное отношение М к (Al+Е) и составляет от 0 до 4,0, R представляет собой органоаммонийный катион, выбранный из группы, состоящей из холина, этилтриметиламмония (ЕТМА), диэтилдиметиламмония (DEDMA), тетраэтиламмония (TEA), тетрапропиламмония (ТРА), триметилпропиламмония, триметилбутиламмония, диметилдиэтаноламмония, гексаметония и их смесей, "r" представляет собой мольное отношение R к (Al+Е) и составляет от 0,25 до 4,0, "n" представляет собой средневзвешенную валентность М и составляет от 1 до 3, "p" представляет собой средневзвешенную валентность R и составляет от 1 до 2, Е представляет собой ...

УЛУЧШЕННЫЙ СПОСОБ АЛКИЛИРОВАНИЯ

... 1. Способ получения потока алкилированного ароматического соединения из по меньшей мере одного необработанного потока способного к алкилированию ароматического соединения, находящегося в жидкой фазе и содержащего каталитические яды, и потока алкилирующего агента, причем указанный необработанный поток способного к алкилированию ароматического соединения обрабатывают с целью снижения содержания каталитических ядов, способ включает следующие стадии:(а) контактирование указанного жидкофазного необработанного потока способного к алкилированию ароматического соединения, содержащего указанные каталитические яды, и потока алкилирующего агента с обрабатывающей композицией в зоне обработки, отдельной от реакционной зоны алкилирования, в условиях обработки с целью удаления по меньшей мере части указанных каталитических ядов и алкилирования по меньшей мере части указанного способного к алкилированию ароматического соединения с получением обработанного отходящего потока, который включает обработанное ...

КАТАЛИТИЧЕСКАЯ СИСТЕМА ДЛЯ ДЕПАРАФИНИЗАЦИИ

КАТАЛИЗАТОР СКВ, ДОПУСКАЮЩИЙ ПЕРЕДОЗИРОВКУ NH3

АЛЮМОСИЛИКАТНЫЙ ЦЕОЛИТ UZM-7, СПОСОБ ЕГО ПОЛУЧЕНИЯ И СПОСОБ ЕГО ИСПОЛЬЗОВАНИЯ

... 1. Микропористый кристаллический цеолит, имеющий трехмерную структуру с по меньшей мере тетраэдрическими единицами AlOи SiOи эмпирическим составом синтезированного безводного продукта, выраженным эмпирической формулой:,где М представляет собой по меньшей мере один обменный катион, выбранный из группы, состоящей из щелочных, щелочноземельных и редкоземельных металлов, "m" представляет собой мольное отношение М к (Al+Е) и варьируется от 0 до приблизительно 2,0, R представляет собой катион органиламмония, выбранный из группы, состоящей из холина, этилтриметиламмония (ЭТМА), диэтилдиметиламмония (ДЭДМА), тетраэтиламмония (ТЭА), тетрапропиламмония (ТПА), триметилпропиламмония, триметилбутиламмония, диметилдиэтаноламмония, гексаметония и их смесей, "r" представляет собой мольное отношение R к (Al+Е) и имеет значение от приблизительно 0,25 до приблизительно 4,0, "n" представляет собой средневзвешенную валентность М и имеет значение от приблизительно 1 до приблизительно 3, "p" представляет собой ...

СПОСОБ АЛКИЛИРОВАНИЯ С ИСПОЛЬЗОВАНИЕМ ЦЕОЛИТА UZM-8

... 1. Способ алкилирования для получения моноалкилированного ароматического соединения, включающий: ! а) пропускание ароматического исходного материала, содержащего исходное ароматическое соединение, олефинового исходного материала, содержащего ! C2-C4олефин, и дополнительного потока, содержащего алкилированное производное исходного ароматического соединения, содержащее от одной до шести дополнительных C2-C4адкильных групп в сравнении с исходным ароматическим соединением, через слой катализатора алкилирования, содержащий твердый катализатор, где твердый катализатор содержит микропористый кристаллический цеолит, имеющий слоистую структуру по меньшей мере из тетраэдрических единиц ! AlO2 и SiO2 и состав, на основе синтезированного безводного продукта, выраженный эмпирической формулой ! Mm n+Rr p+Al1-xExSiyOz, ! где М обозначает по меньшей мере один обмениваемый катион, "m" обозначает отношение М к (Al+Е) и варьируется от 0 до 2,0, R обозначает по меньшей мере один аммонийорганический катион, ...

СИНТЕЗ НОВОГО ЦЕОЛИТА С ИСТОЧНИКОМ ФТОРИДА

ПОЛУЧЕНИЕ АЛЮМОСИЛИКАТНОГО ЦЕОЛИТА AEI

КАТАЛИТИЧЕСКИЙ ФИЛЬТР С ПРОТОЧНЫМИ СТЕНКАМИ, СНАБЖЕННЫЙ МЕМБРАНОЙ

ЦЕОЛИТНЫЕ МАТЕРИАЛЫ И СПОСОБЫ ИХ ПОЛУЧЕНИЯ С ПРИМЕНЕНИЕМ АЛКЕНИЛТРИАММОНИЕВЫХ СОЕДИНЕНИЙ

... 1. Способ получения цеолитного материала, обладающего каркасной структурой типа MFI, включающий стадии:(1) получение смеси, содержащей один или более источников YOи одно или более содержащих алкенилтриалкиламмониевый катион RRRRNсоединений в качестве направляющего реагента для образования структуры; и(2) кристаллизацию смеси, полученной на стадии (1), с получением цеолитного материала;где Y означает четырехвалентный элемент игде R, Rи Rнезависимо друг от друга означают н-пропил; иRозначает 2-пропен-1-ил или 1-пропен-1-ил.2. Способ по п. 1, в котором направляющий реагент для образования структуры, который вводят на стадии (1), представляет собой N-(2-пропен-1-ил)-три-н-пропиламмония гидроксид и/или N-(1-пропен-1-ил)-три-н-пропиламмония гидроксид.3. Способ по п. 1, в котором смесь, полученная на стадии (1), содержит два или более содержащих RRRRNсоединений, где Rв двух или более соединениях отличаются друг от друга и означают 2-пропен-1-ил и 1-пропен-1-ил.4. Способ по п. 3, в котором смесь ...

Способ получения цеолита типа природного левинита

Изобретение относится к способам получения цеолитов, используемых в качестве адсорбентов и катализаторов и позволяет повысить каталитическую активность цеолита в процессе конверсии метанола. Водная смесь имеет следующее молярное соотношение SiO /А1,0д 30-100, 1,0 1,7, НгО/Z 35-175, H O/SiO 10-30, 0,2-0,4. ион металла, ион N - метилхинуклиди- на, Z - гидроксид или кислотный радикйл, образующий соли с ионом хинуклидина, общая щелочь. Полученный гель перемешивают в автоклаве при 95-18(fc, фильтруют, промывают и сушат. 7 табл. СО ...

VERFAHREN ZUR ALKYLIERUNG BENZO-REICHER REFORMIERUNGSPRODUKTE MITTELS MCM-49

Herstellungsverfahren für einen kristallinen, porigen Silikatverbund und seine Anwendung zum katalytischen cracken.

Verfahren zur Reduktion von NO und NO2 in einer oxidierenden Umgebung

Modifizierter Zeolith mit NES Struktur, und seine Verwendung für die Dismutation und/oder Transalkylierung von alkylaromatischen Kohlenwasserstoffen

ZEOLITH ITQ-5

ALUMINIUM-MODIFIZIERTE KIESELSAEURE, VERFAHREN ZU DEREN HERSTELLUNG UND DEREN VERWENDUNG

VERFAHREN ZUR HERSTELLUNG VON KRISTALLINEN UND ZEOLITHISCHEN ALUMOSILIKATEN

Durch Zeolith unterstützter, auf Silber basierender Katalysator zur Speicherung von NOx

Ein Nachbehandlungssystem verwendet chemische Reaktionen, um einen Abgasfluss zu behandeln. Eine Vorrichtung zur Verwendung innerhalb eines Nachbehandlungssystems schließt einen auf Silber basierenden NOx-Speicherkatalysator und einen Zeolithen ein. Der auf Silber basierende NOx-Speicherkatalysator und der Zeolith speichern NOx während einer Niedertemperatur-Betriebsanlaufperiode. In einer Ausführung schließt der Zeolith einen Barium-Y-Zeolithen ein.

KATALYTISCHER WANDSTROMFILTER, DER EINE MEMBRAN AUFWEIST

Die vorliegende Erfindung betrifft einen katalytischen Wandstrom-Monolith zur Verwendung in einem Emissionsbehandlungssystem, wobei der Monolith ein poröses Substrat umfasst und eine erste Fläche und eine zweite Fläche, die eine Längsrichtung dazwischen definieren, und eine erste und eine zweite Vielzahl von Kanälen, die sich in der Längsrichtung erstrecken, aufweist, wobei die erste Vielzahl von Kanälen eine erste Vielzahl von inneren Oberflächen liefert und an der ersten Fläche offen und an der zweiten Fläche geschlossen ist, und wobei die zweite Vielzahl von Kanälen an der zweiten Fläche offen und an der ersten Fläche geschlossen ist, wobei ein erstes katalytisches Material in dem porösen Substrat verteilt ist, wobei eine mikroporöse Membran in der ersten Vielzahl von Kanälen auf einem sich in Längsrichtung erstreckenden ersten Bereich der ersten Vielzahl von inneren Oberflächen bereitgestellt ist, und wobei der erste Bereich sich von der ersten Fläche über 75 % bis 95 % einer Länge ...

VERBESSERTES FLEXIBELES VERFAHREN ZUR HERSTELLUNG VON BASISÖLEN UND MITTELDESTILLATEN MITTELS EINER HYDROISOMERIERUNG UND ANSCHLIESSENDER KATALYTISCHEN ENTPARRAFFINIERUNG

ZEOLITHE UND VERFAHREN ZU IHRER HERSTELLUNG

Verfahren zur Herstellung synthetischer Zeolithe

ZEOLITISCHES MOLEKULARSIEB

Diesel oxidation catalyst and exhaust system

Aei zeolite synthesis

Core-shell catalysts and absorbents

Active inorganic composites are disclosed which have a core-shell structure which comprises a particulate inorganic core and a shell layer comprising a plurality of inorganic shell particles. The composites may be manufactured by methods utilizing charge reversal to ensure that inorganic particulate material of the shell layer is attracted and bonded to the core particle. The materials find use as catalysts and adsorbents and separation media. The core may be a zeolite and the shell layer may be a zeolite or a mixed metal oxide such as a perovskite.

ZEOLITES

CONVERSION OF SYNTHESIS GAS INTO HYDROCARBONS

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).

JMZ-5 zeolites having an SZR-type crystal structure, and methods of their preparation and use

A novel zeolite synthesis with a fluoride source

Provided are a novel synthesis technique for producing pure phase aluminosilicate zeolite and a catalyst comprising the phase pure zeolite in combination with a metal, and methods of using the same.

Selective production of olefins

A lower alcohol and/or ether feed is selectively converted to a mixture of light olefins, including ethylene and propylene, by catalytic contact of the feed material with a catalyst comprising one or more zeolites characterized by a silica to alumina mole ratio of at least 12 and a constraint index in the approximate range of 1 to 12. The catalytic conversion is carried out in the presence of bulky heterocyclic organic nitrogen compounds to suppress the formation of mono-nuclear aromatics. The process of this invention is particularly useful in the production of C2-C3 olefins from methanol or dimethyl ether.

Zeolite promoted v/ti/w catalysts

Provided is a catalyst composition for treating exhaust gas comprising a blend of a first component and second component, wherein the first component is an aluminosilicate or ferrosilicate molecular sieve component wherein the molecular sieve is either in H+ form or is ion exchanged with one or more transition metals, and the second component is a vanadium oxide supported on a metal oxide support selected from alumina, titania, zirconia, ceria, silica, and combinations thereof. Also provided are methods, systems, and catalytic articles incorporating or utilizing such catalyst blends.

Process for producing a catalyst and catalyst as such

Catalyst for treating exhaust gas

Provided is a catalyst composition having an aluminosilicate molecular sieve having an AEI structure and a mole ratio of silica-to-alumina of about 20 to about 30 loaded with about 1 to about 5 weight percent of a promoter metal, based on the total weight of the molecular sieve material. Also provided are method, articles, and systems utilizing the catalyst composition.

Molecular sieve catalyst treatment

METALLOSILICATES

Diesel oxidation catalyst and exhaust system

An oxidation catalyst for treating an exhaust gas from a diesel engine comprising: a first washcoat region comprising platinum, manganese and a first support material; a second washcoat region comprising a platinum group metal and a second support material; and a substrate having an inlet end and an outlet end; wherein the second washcoat region is arranged to contact the exhaust gases at the outlet end of the substrate and after contact of the exhaust gases with first washcoat region. The first washcoat region may be a first washcoat layer and the second washcoat region may be deposited on the first washcoat layer. The support materials may comprise a refractory metal oxide selected from the group consisting of alumina, silica, titania, zirconia, ceria and a mixed or composite oxide of two or more thereof. The refractory metal oxide may be optionally doped with a dopant. An exhaust system, vehicle or apparatus, and method of use comprising the catalyst are also disclosed.

JMZ-5 and JMZ-6, zeolites having an SZR-type crystal structure, and methods of their preparation and use

ZEOLITES

Molecular sieve catalyst for treating exhaust gas

Fischer-tropsch synthesis

Diesel oxidation catalyst and exhaust system

HYDROTHERMALSYNTHESE IN RECEIVERS

SOUR OXIDE WITH MICRO AND MESOPORÖSEN CHARACTERISTICS

HYDROGENATION CATALYSTS

CRYSTALLINE MOLECULAR FILTERS COK-5

PROCEDURE FOR THE PRETREATMENT OF HYDROAMINIERUNGSKATALYSATOREN

PROCEDURE FOR THE PRODUCTION A ALUMINUM MODEFIZIERTEN OF A SILICIC ACID

KATLYTI PROCEDURE FOR THE ENTPARAFFINIEREN OF GAS OIL RAW MATERIAL

NEW ZEOLITE SSZ-31

ZEOLITES

CATALYTIC PROCEDURE FOR THE PRODUCTION OF LUBRICATING OILS WITH LOW SETTING POINT.

PROCEDURE FOR THE CATALYTIC CONVERSION OF HYDROCARBONS USING SYNTHETIC CRYSTALLINE ALUMOSILICATE.

BY ZEOLITES CATALYZED REACTIONS.

CONVERSION CARBON WASSERSTOFFHALTIGEN CONNECTIONS OVER NOT ZEOLITHI CATALYSTS, FRAGMENTED BY CRUDE OILS WITH.

HYDROCARBON CRACKING PROCEDURE.

PRODUCTION OF ZEOLITE L.

MODIFICATION OF ZEOLITES WITH AMMONIUM FLUORIDE.

Process for producing alkylated aromatic compounds and process for producing phenols

According to a process of the invention, a ketone, an aromatic compound and hydrogen as starting materials are reacted together in a single reaction step to produce an alkylaromatic compound in high yield. A process for producing phenols in the invention includes a step of performing the above alkylation process and does not increase the number of steps compared to the conventional cumene process. The process for producing alkylated aromatic compounds includes reacting an aromatic compound such as benzene, a ketone such as acetone and hydrogen in the presence of a solid acid substance, preferably a zeolite, and a silver-containing catalyst.

Olefin production process

A novel olefin production process is provided which can be established as an industrial and practical process capable of producing olefins by directly reacting a ketone and hydrogen in a single reaction step. In particular, a novel olefin production process is provided in which propylene is obtained with high selectivity by directly reacting acetone and hydrogen. The olefin production process according to the present invention includes reacting a ketone and hydrogen in the presence of at least one dehydration catalyst and a silver-containing catalyst, and the at least one dehydration catalyst is selected from metal oxide catalysts containing a Group 6 element, zeolites, aluminas and heteropoly acid salts in which part or all the protons in heteropoly acids are exchanged with metal cations.

Process for producing aromatic hydrocarbon and transition-metal-containing crystalline metallosilicate catalyst for use in the production process

Provided is a process for producing an aromatic hydrocarbon efficiently at high yield from a lower hydrocarbon containing methane as a major component, and such a process for producing an aromatic hydrocarbon includes the step of reacting a lower hydrocarbon containing methane as a major component in the presence of a transition-metal-containing crystalline metallosilicate catalyst which is obtainable by supporting 5 to 25 parts by weight of a transition metal (X) on 100 parts by weight of a modified crystalline metallosilicate obtainable by subjecting a crystalline metallosilicate to a series of treatment (A) including a step (i) of eliminating part of a metal from the crystalline metallosilicate and a silylation step (ii).

Process For Producing Cyclohexylbenzene

In a process for producing cyclohexylbenzene, benzene and hydrogen are contacted under hydroalkylation conditions with a catalyst system comprising a MCM-22 family molecular sieve and at least one hydrogenation metal. The conditions comprise a temperature of about 140° C. to about 175° C., a pressure of about 135 psig to about 175 psig (931 kPag to 1207 kPag), a hydrogen to benzene molar ratio of about 0.30 to about 0.65 and a weight hourly space velocity of benzene of about 0.26 to about 1.05 hr −1 .

Molecular Sieve Of MFS Framework Type With Controllable Average Size, Its Method of Making And Use

A method of making a crystalline molecular sieve of MFS framework type, preferably ZSM-57, from a synthesis mixture comprising at least one source of tetravalent element (Y), at least one source of trivalent element (X), at least one source of alkali metal hydroxide (MOH), at least one structure-directing-agent (R) and water, said alkali metal (M) comprising potassium, and having the following mole composition (expressed in terms of oxide): YO 2 :( p )X 2 O 3 :( q )OH − :( r )R:( s )H 2 O, wherein (p) is in the range from 0.005 to 0.05, (q) is in the range from 0.01 to 3, (r) is in the range from 0.03 to 2 and (s) is in the range from 10 to 75 (based on total weight of said synthesis mixture); wherein the crystals of molecular sieve formed having an average diameter (D) of less than or equal to 1.5 micron and an average thickness (T) of less than or equal to 300 nanometers.

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.

Molecular Sieve Composition (EMM-10), Its Method of Making, and Use for Hydrocarbon Conversions

This invention relates to a process for hydrocarbon conversion comprising contacting a hydrocarbon feedstock with a crystalline molecular sieve, in its ammonium exchanged form or in its calcined form, under conversion conditions to form a conversion product, said crystalline molecular sieve comprising unit cells with MWW topology and is characterized by diffraction streaking from the unit cell arrangement in the c direction as evidenced by the arced hk0 patterns of electron diffraction pattern.

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.

SYNTHESIS OF MSE-FRAMEWORK TYPE MOLECULAR SIEVES

An aspect of the invention relates to a method of synthesizing a crystalline molecular sieve having an MSE framework type, the method comprising crystallizing a reaction mixture comprising a source of water, a source of an oxide of a tetravalent element, Y, selected from at least one of silicon, tin, titanium, vanadium, and germanium, optionally but preferably a source of a trivalent element, X, a source of an alkali or alkaline earth metal, M, a source of a first single-nitrogen-containing cyclic ammonium organic cation, Q1, and optionally a source of a second multiple-nitrogen-containing organic cation, Q2, which can include multiple-nitrogen-containing monocations and/or multiply ionic species containing two or more ammonium cations in the same molecule. 2. The method of claim 1 , wherein the at least 3 of the R-Rgroups or the R-Rgroups are hydrogen claim 1 , and wherein at least one of the Rand Rgroups or at least one of the Rand Rgroups is a methyl and/or ethyl group.3. The method of claim 1 , wherein the first organic cation claim 1 , O| claim 1 , comprises or is a six-membered nitrogen-containing ring claim 1 , A is a >CRRgroup claim 1 , all the R-Rand R-Rgroups are hydrogen claim 1 , and the Rand Rgroups together have a number of carbon atoms that sum to between 2 and 6.4. The method of claim 1 , wherein the first organic cation claim 1 , Q1 claim 1 , comprises or is a six-membered nitrogen-containing ring claim 1 , A is an >O group claim 1 , all the R-Rand R-Rgroups are hydrogen claim 1 , and the Rand Rgroups together have a number of carbon atoms that sum to between 2 and 6.5. The method of claim 1 , wherein the first organic cation claim 1 , Q1 claim 1 , comprises or is a six-membered nitrogen-containing ring claim 1 , A is >CRRgroup claim 1 , all but one of the R-Rgroups are hydrogen claim 1 , the one of the R-Rgroups that is not hydrogen is connected to one of the R-Rgroups claim 1 , forming a bicyclic ring system claim 1 , and the other of the R- ...

Synthesis of mse-framework type molecular sieves

A method of synthesizing a crystalline molecular sieve having an MSE framework type comprises crystallizing a reaction mixture comprising a source of water, a source of an oxide of a tetravalent element, Y, selected from at least one of silicon, tin, titanium, vanadium, and germanium, optionally a source of a trivalent element, X, a source of an alkali or alkaline earth metal, M, and a source of organic dications, Q, such as 3-hydroxy-1-(4-(1-methylpiperidin-1-ium-1 yl)butyl)quinuclidin-1-ium, 3-hydroxy-1-(5-(1-methylpiperidin-1-ium-1-yl)pentyl)quinuclidin-1-ium, 1,1′-(butane-1,4-diyl)bis(1-methylpiperidin-1-ium), 1,1′-(pentane-1,5-diyl)bis(1-methylpiperidin-1-ium), 1,1′-(hexane-1,6-diyl)bis(1-methylpiperidin-1-ium), and 1,1′-((3as,6as)-octahydropentalene-2,5-diyl)bis(1-methylpiperidin-1-ium).

ORGANOTEMPLATE-FREE SYNTHETIC PROCESS FOR THE PRODUCTION OF A ZEOLITIC MATERIAL

The present invention relates to an organotemplate-free synthetic process for the production of a zeolitic material having a BEA framework structure comprising YOand optionally comprising XO, wherein said process comprises the steps of (1) preparing a mixture comprising seed crystals and at least one source for YO; and (2) crystallizing the mixture; wherein Y is a tetravalent element, and X is a trivalent element, wherein the zeolitic material optionally comprises at least one alkali metal M, wherein when the BEA framework additionally comprises XO, the mixture according to step (1) comprises at least one source for XO, and wherein the seed crystals comprise zeolitic material having a BEA framework structure, preferably zeolite Beta. 1. An organotemplate-free synthetic process for the production of a zeolitic material having a BEA framework structure comprising YOand optionally comprising XO , wherein said process comprises{'sub': '2', '(1) preparing a mixture comprising seed crystals, at least one source for YO; and'}(2) crystallizing the mixture,wherein Y is a tetravalent element, and X is a trivalent element,wherein the zeolitic material optionally comprises at least one alkali metal M,{'sub': 2', '3', '2', '3, 'wherein when the BEA framework additionally comprises XO, the mixture according to step (1) comprises at least one source for XO, and'}wherein the seed crystals comprise zeolitic material having a BEA framework structure.2. The process according to claim 1 , wherein Y is selected from the group consisting of Si claim 1 , Sn claim 1 , Ti claim 1 , Zr claim 1 , Ge claim 1 , and a mixture of two or more thereof.3. The process according to claim 1 , wherein the at least one source for YOcomprises at least one silicate.4. The process according to claim 3 , wherein the at least one source for YOcomprises water glass.5. The process according to claim 1 , wherein X is selected from the group consisting of Al claim 1 , B claim 1 , In claim 1 , Ga claim 1 , and a ...

Process for Ion Exchange on Zeolites

Aspects of the present invention relate to an improved process for exchanging alkali metal or alkaline earth metal ions in zeolites for ammonium ions. For this exchange, aqueous solutions of ammonium salts, for example ammonium sulfate, ammonium nitrate or ammonium chloride, are currently being used. The resulting “ammonium zeolites” are calcined to convert them, with release of ammonia, to the H form of the zeolites suitable as a catalyst. Certain methods provided herein use ammonium carbonate instead of the ammonium compounds mentioned. As excess ammonium carbonate, in contrast to the nitrates, sulfates or chlorides, can be recycled in the form of carbon dioxide and ammonia, the amount of salt which has to be discharged is lowered significantly.

Stabilized microporous crystalline material, the method of making the same, and the use for selective catalytic reduction of nox

There is disclosed a microporous crystalline material having pore opening ranging from 3 to 5 Angstroms, where the material comprises a first metal chosen from alkali earth group, rare earth group, alkali group, or mixtures thereof, and a second metal chosen from iron, copper or mixtures thereof; and has a molar silica to alumina ratio (SAR) from 3 to 10. The microporous crystalline material disclosed herein may comprise a crystal structure having building units of double-6-rings (d6r) and pore opening of 8-rings as exemplified with framework types defined by the Structure Commission of the International Zeolite Association having structural codes of CHA, LEV, AEI, AFT, AFX, EAB, ERI, KFI, SAT, TSC, and SAV. There is also disclosed a method of selective catalytic reduction of nitrogen oxides in exhaust gas, comprising at least partially contacting the exhaust gases with an article comprising the disclosed microporous crystalline material.

METHOD FOR PRODUCING MTW-TYPE ZEOLITE

The method for producing an MTW-type zeolite according to the present invention includes: mixing a silica source, an alumina source, an alkali source, a lithium source, and water so as to obtain a reaction mixture having a composition represented by specific molar ratios; (2) adding an MTW-type zeolite which has a SiO/AlOratio of 10 to 500 and does not contain an organic compound, as a seed crystal, to the reaction mixture in a proportion of 0.1 to 20% by weight relative to the silica component in the reaction mixture; and (3) airtightly heating the reaction mixture, to which the seed crystal has been added, at 100 to 200° C. 1. A method for producing an MTW-type zeolite , comprising: [{'sub': 2', '2', '3, 'SiO/AlO=12 to 200'}, {'sub': 2', '2, 'NaO/SiO=0.1 to 0.3'}, {'sub': 2', '2', '2, 'LiO/(NaO+LiO)=0.05 to 0.5'}, {'sub': 2', '2, 'HO/SiO=10 to 50;'}], '(1) mixing a silica source, an alumina source, an alkali source, a lithium source, and water so as to obtain a reaction mixture having a composition represented by the following molar ratios{'sub': 2', '2', '3, '(2) adding an MTW-type zeolite which has a SiO/AlOratio of 10 to 500 and does not contain an organic compound, as a seed crystal, to the reaction mixture in a proportion of 0.1 to 20% by weight relative to the silica component in the reaction mixture; and'}(3) airtightly heating the reaction mixture, to which the seed crystal has been added, at 100 to 200° C.2. The production method according to , wherein a beta-type zeolite produced by the production method according to is used as a seed crystal. The present invention relates to a method for producing an MTW-type zeolite from a reaction mixture in which an organic compound is not used, by adding an MTW-type zeolite which does not contain an organic compound, as a seed crystal.Synthetic zeolite is a crystalline aluminosilicate and has uniform micropores in an angstrom size resulting from the crystal structure thereof. Taking advantage of this feature, the ...

UZM-39 ALUMINOSILICATE ZEOLITE

A new family of coherently grown composites of TUN and IMF zeotypes have been synthesized. These zeolites are represented by the empirical formula. 2. The process of further comprising modifying the coherently grown composite using a technique selected from the group consisting of calcination claim 1 , ion-exchange claim 1 , steaming claim 1 , acid treatment claim 1 , acid extraction claim 1 , and combinations thereof.3. The process of wherein L is at least one microporous layered zeolite with crystal thickness in at least one dimension of less than about 30 to about 50 nm.4. The process of wherein L is at least one microporous layered zeolite with pore diameters of less than about 2 nm.6. The process of wherein L is at least one microporous layered zeolite with crystal thickness in at least one dimension of less than about 30 to about 50 nm.7. The process of wherein L is at least one microporous layered zeolite with pore diameters of less than about 2 nm.8. The process of further comprising modifying the coherently grown composite using a technique selected from the group consisting of calcination claim 5 , ion-exchange claim 5 , steaming claim 5 , acid treatment claim 5 , acid extraction claim 5 , and combinations thereof. This application claims priority from Provisional Application No. 61/578,909 filed Dec. 22, 2011, the contents of which are hereby incorporated by reference.This invention relates to a new family of aluminosilicate zeolites designated UZM-39. They are represented by the empirical formula of:NaMTAlESiOwhere M represents a metal or metals from zinc or Group 1 (IUPAC 1), Group 2 (IUPAC 2), Group 3 (IUPAC 3) or the lanthanide series of the periodic table, T is the organic directing agent derived from reactants R and Q where R is an A,Ω-dihalosubstituted alkane such as 1,4-dibromobutane and Q is at least one neutral amine having 6 or fewer carbon atoms such as 1-methylpyrrolidine. E is a framework element such as gallium.Zeolites are crystalline ...

Uzm-39 aluminosilicate zeolite

A new family of coherently grown composites of TUN and IMF zeotypes have been synthesized. These zeolites are represented by the empirical formula. Na n M m k+ T t Al 1−x E x Si y O z where “n” is the mole ratio of Na to (Al+E), M represents a metal or metals from zinc, Group 1, Group 2, Group 3 and or the lanthanide series of the periodic table, “m” is the mole ratio of M to (Al+E), “k” is the average charge of the metal or metals M, T is the organic structure directing agent or agents, and E is a framework element such as gallium. These zeolites are similar to TNU-9 and IM-5 but are characterized by unique compositions and synthesis procedures and have catalytic properties for carrying out various hydrocarbon conversion processes and separation properties for carrying out various separations.

Supported nano sized zeolite catalyst for alkylation reactions

A catalyst containing nanosize zeolite particles supported on a support material for alkylation reactions, such as the alkylation of benzene to form ethylbenzene, and processes using such a catalyst is disclosed.

ZEOLITE OR AN ANALOGOUS MATERIAL THEREOF INCLUDING MESOPORES ARRANGED REGULARLY OR IRREGULARLY, AND PREPARATION METHOD FOR SAME

The present invention relates to a novel zeolite or zeolite-like material synthesized using a zeolite synthesis composition comprising a specifically designed organic surfactant, wherein the zeolite or zeolite-like material comprises a crystalline framework having a thickness corresponding to up to 10 single unit cells along at least one axis, and 2-50 nm mesopores formed by organic assembly of the crystalline framework are regularly or irregularly arranged in the zeolite or zeolite-like material. In addition, the present invention presents a micro-mesoporous molecular sieve material activated or functionalized by dealumination, ion exchange or other post-treatment processes, and a method of using the molecular sieve material as a catalyst. The disclosed novel materials have a significantly increased outer surface area and pore volume due to a combination of micropores and mesopores, and thus show an increased diffusion of molecules therein. Accordingly, these materials will exhibit significantly increased activities compared to conventional zeolite catalysts and ion exchange resins. 1. A zeolite or zeolite-like material comprising:a crystalline framework which comprises micropores having a size of 2 nm or less and has a thickness to corresponding to up to 10 single unit cells along at least one axis; andmesopores formed by self-assembly of the crystalline framework and having a size of 2 nm or more.2. The zeolite or zeolite-like material of claim 1 , wherein the mesopores are hexagonally ordered.3. The zeolite or zeolite-like material of claim 1 , wherein the mesopores are cubically ordered.4. The zeolite or zeolite-like material of claim 1 , wherein the mesopores are disordered.5. The zeolite or zeolite-like material of claim 1 , wherein the crystalline framework includes a metal element selected from the group consisting of Be claim 1 , B claim 1 , Al claim 1 , Ti claim 1 , Fe claim 1 , Ga claim 1 , V claim 1 , Cr claim 1 , Co claim 1 , Ni claim 1 , Cu claim 1 , ...

Diesel oxidation catalyst

The present invention relates to a catalytically active material consisting of an inner core ( 1 ) and an outer shell ( 2 ) surrounding this core, the core being formed from palladium and gold fixed together on a first support oxide, and the shell comprising platinum fixed on a second support oxide, to a diesel oxidation catalyst comprising this catalytically active material, and to an exhaust gas cleaning system comprising this diesel oxidation catalyst.

Binderless Molecular Sieve Catalyst and a Preparation Method Thereof

The present invention relate to a binderless molecular sieve catalyst and a process for preparing the same, which are mainly useful for solving the problems of the current catalysts, such as lower activity, less pore volume and worse diffusivity. The present invention relates to a novel binderless molecular sieve catalyst, comprising, based on the weight of the catalyst, 90-100 wt. % of a molecular sieve, 0-10 wt. % of a binder, and 0-10 wt. % of an anti-wear agent, wherein said catalyst has a pore volume of 0.1-0.5 ml/g, an average pore diameter of 50-100 nm, and a porosity of 20-40%; the anti-wear agent is selected from the rod or needle-like inorganic materials having a length/diameter ratio of 2-20. Said catalyst has the advantages of higher activity, greater pore volume, larger average pore diameter and porosity, and better diffusivity, and well solves said problems and can be used for the industrial preparation of binderless molecular sieve catalysts. 1. A binderless molecular sieve catalyst , comprising , based on the weight of the catalyst , 90-100 wt. % of a molecular sieve , 0-10 wt. % of a binder , and 0-10 wt. % of an anti-wear agent , wherein said catalyst has a pore volume of 0.10-0.52 ml/g , an average pore diameter of 50-100 nm , and a porosity of 20-40%; the anti-wear agent is selected from the rod or needle-like inorganic materials having a length/diameter ratio of 2-20.2. The binderless molecular sieve catalyst according to claim 1 , characterized in that the catalyst has a pore volume of 0.15-0.3 ml/g claim 1 , an average pore diameter of 50-70 mm claim 1 , and a porosity of 20-30%.3. The binderless molecular sieve catalyst according to claim 1 , characterized in that the catalyst has a pore volume of 0.31-0.5 ml/g claim 1 , an average pore diameter of 71-100 nm claim 1 , and a porosity of 31-40%.4. The binderless molecular sieve catalyst according to claim 1 , characterized in that the molecular sieve in the binderless molecular sieve catalyst ...

Liquid Phase Alkylation Process

The present invention provides a process for producing a monoalkylated aromatic compound comprising the step of contacting an alkylatable aromatic compound with an alkylating agent in the presence of a catalyst composition under effective alkylation conditions, said catalyst composition comprising MCM-56 and a binder, such that the crystal/binder weight ratio in the catalyst composition is from above 20/80 to about 80/20. 1. A process for producing a monoalkylated aromatic compound comprising the step of contacting an alkylatable aromatic compound with an alkylating agent in the presence of a catalyst composition under effective alkylation conditions , said catalyst composition comprising MCM-56 and a binder , such that the crystal/binder weight ratio in the catalyst composition is from above 20/80 to about 80/20.2. The process of claim 1 , wherein said crystal/binder weight ratio in said catalyst composition is from about 40/60 to about 80/20.3. The process of claim 1 , wherein said crystal/binder weight ratio in said catalyst composition is from about 40/60 to about 60/40.4. The process of claim 1 , wherein said binder is a synthetic or naturally occurring inorganic material selected from the group consisting of alumina claim 1 , clay claim 1 , silica and/or metal oxides.5. The process of claim 1 , wherein said alkylatable aromatic compound is benzene claim 1 , said alkylating agent is ethylene and said monoalkylated aromatic compound is ethylbenzene.6. The process of claim 1 , wherein said alkylatable aromatic compound is benzene claim 1 , said alkylating agent is propylene and said monoalkylated aromatic compound is cumene.8. The process of claim 7 , wherein the crystal/binder weight ratio is from about 40/60 to about 80/20 or from about 40/60 to about 60/40.9. The process of claim 7 , wherein said product in step (c) further comprising dialkylated benzene and trialkylated benzene claim 7 , and the weight ratio of trialkylated benzene to dialkylated benzene is ...

Catalysts Useful for the Alkylation of Aromatic Hydrocarbons

A catalyst useful for the alkylation or transalkylation of aromatic compounds is disclosed. The catalyst is an acid-treated zeolitic catalyst produced by a process including contacting an acidic zeolitic catalyst comprising surface non-framework aluminum and framework aluminum with an organic dibasic acid at a catalyst to acid weight ratio in the range from about 2:1 to about 20:1 and at a temperature in the range from about 50° C. to about 100° C. to selectively remove at least a portion of the surface non-framework aluminum. The resulting catalyst may have a measured first-order rate constant, k cum , for the alkylation of benzene with propylene to form cumene, of at least 2.0 cm 3 /s g.

Silica composite, method for producing the same, and method for producing propylene using the silica composite

The present invention provides a method for producing a silica composite by the steps of: preparing a raw material mixture containing silica and zeolite; drying the raw material mixture to obtain a dried product; and calcining the dried product, wherein the method comprising the step of allowing the raw material mixture to contain phosphoric acid and/or phosphate or bringing a solution of phosphoric acid and/or phosphate into contact with the zeolite and/or the dried product, or a combination thereof to thereby adjust a phosphorus content in the silica composite to 0.01 to 1.0% by mass based on the total mass of the silica composite.

ZEOLITE SCR CATALYSTS WITH IRON OR COPPER

Cu/mordenite catalysts were found to be highly active for the SCR of NO with NHand exhibited high resistance to alkali poisoning. Redox and acidic properties of Cu/mordenite were well preserved after poisoning with potassium unlike that of vanadium catalysts. Fe-mordenite catalysts also revealed much higher alkali resistivity than that of commercial VO/WO—TiO(VWT) SCR catalyst which is currently used for NOabatement in stationary installations. Unique support properties like high surface area and surface acidity, which are not available in the commercial VWT catalyst, seem to be essential requirements for the high alkali resistance. Mordenite-type zeolite based catalysts could therefore be attractive alternatives to conventional SCR catalysts for biomass fired power plant flue gas treatment. 112.-. (canceled)14. The method according to claim 13 , wherein the Cu precursor is copper nitrate.15. The method according to claim 13 , wherein the zeolite support is HMORDENITE (400 m/g).16. The method according to claim 13 , wherein the zeolite support is HMORDENITE (400 m/g) obtained by protonation of the ammonia form CBV21A zeolite support from Zeolyst International.17. A zeolite catalyst obtainable by a method according to .18. A catalyst according to claim 17 , which comprises 4% w/w Cu.19. A catalyst according to claim 17 , wherein the catalyst is shaped as a monolith claim 17 , extrudate claim 17 , bead claim 17 , plate claim 17 , sheet or fibrous cloth.20. A method of selectively removing nitrogen oxides with ammonia from gases resulting from the burning of biomass claim 17 , combined biomass-fossil fuel claim 17 , or emerging from waste incineration units at a temperature from 320 to 550° C. comprising providing a zeolite catalyst according to .21. The method according to claim 20 , wherein said gases contain between 200-1000 mg KCl/Nm.22. The method according to claim 20 , wherein said gases contain between 10-15% H0.23. The method according to claim 20 , wherein ...

PROCESS FOR THE PRODUCTION OF METAL DOPED ZEOLITES AND ZEOTYPES AND APPLICATION OF SAME TO THE CATALYTIC REMEDIATION OF NITROGEN OXIDES

The present invention is directed to a process for the production of ion-exchanged (metal-doped, metal-exchanged) Zeolites and Zeotypes, In particular, the method applied uses a sublimation step to incorporate the ion within the channels of the Zeolitic material. Hence, according to this dry procedure no solvent is involved which obviates certain drawbacks connected with wet exchange processes known in the art. 2. Process according to claim 1 , wherein the Zeolites or Zeotypes are selected from the group consisting of one or a mixture of Faujasite type claim 1 , Pentasil type claim 1 , Chabazite Zeolite or Zeotype e.g. SAPO-34 or other ‘8-ring’ structures of the structure type CHA and related structure types e.g. AEI claim 1 , AFT claim 1 , AFX claim 1 , DDR claim 1 , ERI claim 1 , ITE claim 1 , ITW claim 1 , KFI claim 1 , LEV claim 1 , LTA claim 1 , PAU claim 1 , RHO claim 1 , and UFI.3. Process according to claim 1 , wherein the metal is selected from the group of Fe claim 1 , Cu claim 1 , Co claim 1 , Ag claim 1 , and Ce.4. Process according to claim 1 , wherein the complex ligand is selected from one or a mixture of the group comprising a diketonate-structure and carbonyl species.5. Process according to claim 1 , wherein the mixture is calcined at a temperature of ≧200° C.-650° C.6. Process according to claim 1 , wherein the mixture is calcined at a temperature of 350-450° C. for 1-5 hours.7. Process according to claim 1 , wherein the mixture comprises the Zeolite or Zeotype material and the precursor compound to provide a subsequent metal dopant loading of 0.01 wt % metal to 10 wt % metal.8. A material or mixture of materials produced according to .9. A catalyst comprising the material or mixture of materials according to claim 8 , wherein the catalyst comprises an inert refractory binder selected from the group consisting of alumina claim 8 , titania claim 8 , non-Zeolitic silica-alumina claim 8 , silica claim 8 , zirconia and mixtures thereof coated on a flow ...

Selecting an Improved Catalyst Composition and Hydrocarbon Conversion Process Using Same

The present invention provides a method for selecting an improved catalyst composition comprising a crystalline molecular sieve material having a structure and properties whereby the catalyst composition has at least one active catalytic site with a Mono Alkylation Selectivity Factor (MASF) greater than or equal to 0 kcal/mol±0.5 kcal/mol, and optionally further at least one active catalytic site with an Olefin Oligomerization Suppression Factor (OOSF) greater than or equal to 5 kcal/mol±0.5 kcal/mol. Further, there is provided an improved process for conversion of hydrocarbon feedstock in the presence of said selected catalyst composition. 1. A method for selecting a catalyst composition comprising a porous crystalline material for use in a hydrocarbon conversion process , said method comprising steps of determining a Mono Alkylation Selectivity Factor of one or more catalyst compositions , and selecting a catalyst composition which has at least one active catalytic site with said Mono Alkylation Selectivity Factor greater than or equal to 0 kcal/mol±0.5 kcal/mol.2. The method of claim 1 , wherein said selected catalyst composition has at least one active catalytic site with a Mono Alkylation Selectivity Factor greater than or equal to 3 kcal/mol±0.5 kcal/mol claim 1 , or greater than or equal to 7 kcal/mol±0.5 kcal/mol.3. The method of claim 1 , further comprising steps of determining a Olefin Oligomerization Suppression Factor of one or more catalyst compositions claim 1 , and selecting a catalyst composition which has at least one active catalytic site with said Olefin Oligomerization Suppression Factor greater than or equal to 5 kcal/mol±0.5 kcal/mol claim 1 , or greater than or equal to 7 kcal/mol±0.5 kcal/mol claim 1 , or greater than or equal to 10 kcal/mol±0.5 kcal/mol.4. The method of claim 1 , wherein said Mono Alkylation Selectivity Factor (MASF) is defined by the formula:{'br': None, 'sup': T', 'Olefin+MonoAlkylated Aromatics', 'T', 'Olefin+Aromatics, ' ...

MECHANOCHEMICAL PRODUCTION OF ZEOLITES

The subject of the invention is a method for the synthesis of zeolites, comprising the following steps: a) providing a silicon source; b) providing an aluminium source; c) optionally providing at least one template; d) mixing the silicon source, aluminium source and optional template in order to produce a synthesis gel; e) grinding the synthesis gel; f) treating the ground synthesis gel under hydrothermal conditions in order to produce crystalline zeolite, as well as zeolites that can be obtained according to this method. The products obtained according to the method can be used as catalysts or catalyst supports. 1. Method for synthesis of zeolites , comprising the following steps:a) providing a silicon source;b) providing an aluminium source;c) mixing the silicon source and the aluminium source in order to produce a synthesis gel;d) grinding the synthesis gel;e) treating the ground synthesis gel under hydrothermal conditions in order to produce a crystalline zeolite.2. Method according to claim 1 , characterized in that the silicon source claim 1 , the aluminium source claim 1 , and the synthesis gel are present in an aqueous medium.3. Method according to claim 1 , characterized in that the silicon source comprises precipitated silicic acid.4. Method according to claim 1 , characterized in that the silicon source and the aluminium source are subjected to grinding.5. Method according to claim 1 , characterized in that the grinding is carried out with at least one grinding device claim 1 , wherein the at least one grinding device is selected from the group consisting of a ball mill claim 1 , an annular gap mill claim 1 , a bead mill claim 1 , a Manton-Gaulin mill claim 1 , and combinations thereof.6. Method according to claim 1 , characterized in that the grinding is carried out at a pH in the range from approximately 9 to 14.7. (canceled)8. Method according to claim 1 , characterized in that after treatment under hydrothermal conditions claim 1 , the obtained ...

Catalyst Composition and Its Use Thereof in Aromatics Alkylation

This disclosure relates to a catalyst composition comprising (a) MCM-22 family material; and (b) a binder comprising at least 1 wt.% of a titanium compound based on the weight of said catalyst composition, wherein said titanium compound was anatase and rutile phases. 1. A catalyst composition comprising:(a) a MCM-22 family material; and(b) a binder comprising a titanium compound in the range from about 1 wt.% to about 35 wt.% based on the weight of said catalyst composition, wherein said titanium compound has anatase and rutile phases.2. The catalyst composition of claim 1 , wherein said titanium compound comprises at least one of titanium oxide claim 1 , titanium hydroxide claim 1 , titanium sulfate claim 1 , titanium phosphate claim 1 , or any combination thereof.3. The catalyst composition of claim 1 , further comprising a different claim 1 , second crystalline MCM-22 family molecular sieve claim 1 , wherein said second crystalline MCM-22 family molecular sieve comprises at least one of MCM-36 claim 1 , MCM-49 claim 1 , MCM-56 claim 1 , EMM-10 family molecular sieve claim 1 , ITQ-1 claim 1 , ITQ-2 claim 1 , ITQ-30 claim 1 , or any combination thereof.4. The catalyst composition of claim 1 , further comprising a molecular sieve having a framework type of at least one of FAU claim 1 , *BEA claim 1 , MFI claim 1 , MTW claim 1 , or any combination thereof.5. The catalyst composition of claim 1 , wherein said MCM-22 family material comprises at least one of MCM-22 claim 1 , MCM-36 claim 1 , MCM-49 claim 1 , MCM-56 claim 1 , EMM-10 family molecular sieve claim 1 , ITQ-1 claim 1 , ITQ-2 claim 1 , and ITQ-30.6. The catalyst composition of claim 1 , having at least 65 wt.% of said MCM-22 family material based on the weight of said catalyst composition.7. The catalyst composition of claim 1 , having at least 80 wt.% of said crystalline MCM-49 molecular sieve based on the eight of said catalyst composition.8. The catalyst composition of claim 1 , wherein said binder has ...

Catalyst Regeneration Process

This disclosure relates to a process for regenerating a catalyst composition to improve the aging rate in subsequent cycles. 1. In a process for conversion of an aromatic hydrocarbon feed stream , including contacting said feed stream with a molecular sieve and carrying out said contacting for a cycle time , whereby coke deposits on said catalyst during at least a portion of said cycle time and wherein the reactor temperature is increased and/or through-put is decreased over at least a portion of said cycle time in order to meet at least one predetermined indicia of conversion efficiency , the improvement comprising determining the end of cycle time by at least one of (i) wt % coke deposits on said molecular sieve , and (ii) H/C ratio of the coke deposits on said molecular sieve.2. The process of claim 1 , including determining end of cycle conditions of said molecular sieve claim 1 , said end of cycle conditions selected from (i) wt % coke deposits on said molecular sieve claim 1 , and (ii) H/C ratio of the coke deposits on said molecular sieve; then regenerating or rejuvenation said molecular sieve and carrying out said contacting for another cycle time claim 1 , with the proviso that said end of cycle conditions change from the previous cycle time; then making a determination of appropriate end of cycle conditions and operating said process based on said determination claim 1 , wherein the improvement is further characterized by a decrease in molecular sieve aging rate claim 1 , expressed as the rate of increase in temperature required to maintain at least one indicia of conversion efficiency constant.3. The process of claim 1 , including regenerating or rejuvenating said catalyst by treatment under oxidative conditions claim 1 , reductive conditions claim 1 , treatment with steam claim 1 , and combinations thereof.4. The process of claim 1 , wherein said conversion process is selected from transalkylation claim 1 , disproportionation claim 1 , comproportionation ...

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.

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 contains crystalline aluminosilicate and a rare earth element, in which the amount of the rare earth element expressed in terms of the element is 0.1 to 10 mass % based on the crystalline aluminosilicate. In the production method of monocyclic aromatic hydrocarbons, oil feed stock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower is brought into contact with the catalyst for producing monocyclic aromatic hydrocarbons. 1. A catalyst for producing monocyclic aromatic hydrocarbons that 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 comprising:crystalline aluminosilicate; anda rare earth element,wherein the amount of the rare earth element that is expressed in terms of the element is 0.1 to 10 mass % based on the crystalline aluminosilicate.2. A catalyst for producing monocyclic aromatic hydrocarbons that 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 comprising: a binder; and', 'a rare earth element,', 'wherein the amount of the rare earth element that is expressed in terms of the element is 0.1 to 30 mass % based on the weight of the catalyst., 'crystalline aluminosilicate;'}3. The catalyst for producing monocyclic aromatic hydrocarbons according to claim 1 , further comprising gallium and/or zinc.4. The ...

HYDROCARBON CONVERSION CATALYST COMPOSITION

A hydrocarbon conversion catalyst composition which comprises ZSM-48 and/or EU-2 zeolite particles and refractory oxide binder essentially free of alumina in which the average aluminium concentration of the ZSM-48 and/or EU-2 zeolite particles is at least 1.3 times the aluminium concentration at the surface of the particles, processes for preparing such catalyst compositions and processes for converting hydrocarbon feedstock with the help of such compositions. 1. A hydrocarbon conversion catalyst composition , which comprises: ZSM-48 and/or EU-2 zeolite particles; and refractory oxide binder essentially free of alumina , in which the average aluminium concentration of the ZSM-48 and/or EU-2 zeolite particles is at least 1.1 times the aluminium concentration at the surface of the particles.2. A hydrocarbon conversion catalyst composition , in which the ZSM-48 and/or EU-2 zeolite has a silica to alumina molar ratio of at least 100 and at most 250.3. A hydrocarbon conversion catalyst composition according to claim 1 , wherein the zeolite content claim 1 , on a dry basis claim 1 , is of from 20 to 70 wt % as calculated on the total finished catalyst composition.4. A hydrocarbon conversion catalyst composition according to in which the average aluminium concentration of the ZSM-48 and/or EU-2 zeolite particles is at least 2 times the aluminium concentration at the surface of the particle.5. A process for preparing a hydrocarbon conversion catalyst composition according to claim 1 , which process comprises contacting the ZSM-48 and/or EU-2 zeolite with a solution of a fluor containing salt.6. A process for preparing a catalytic metal containing hydrocarbon conversion catalyst which process comprises preparing a hydrocarbon conversion catalyst composition according to and incorporating acatalytic metal into the catalyst composition.7. A process for converting a hydrocarbon feedstock which process comprises contacting the feedstock with a catalyst composition according to ...

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

The catalyst for producing aromatic hydrocarbon is for producing monocyclic aromatic hydrocarbon 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 and contains crystalline aluminosilicate and phosphorus. A molar ratio (P/Al ratio) between phosphorus contained in the crystalline aluminosilicate and aluminum of the crystalline aluminosilicate is from 0.1 to 1.0. The production method of monocyclic aromatic hydrocarbon is a method of bringing oil feedstock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower into contact with the catalyst for producing monocyclic aromatic hydrocarbon.

Distillate oil hydrogenation deacidification catalyst containing molecular sieve, preparation and use thereof

Provided are a distillate oil hydrogenation deacidification catalyst containing a molecular sieve, preparation and use thereof. In this catalyst, the weight of the catalyst, on the basis of 100%, is 1-5% magnesium calculated as an oxide, 1-20% alumino-phosphate molecular sieve and/or aluminosilicate molecular sieve; 1-10% Co and/or Ni; 5-30% Mo and/or W, and the balance is aluminium oxide. The catalyst is prepared through forming, dipping and baking. The catalyst is very active in hydrogenation deacidification, and also in hydrodesulfurization and hydrodenitrogenation.

FIBROUS SUBSTRATE-BASED HYDROPROCESSING CATALYSTS AND ASSOCIATED METHODS

Catalysts are disclosed comprising fibrous substrates having silica-containing fibers with diameters generally from about 1 to about 50 microns, which act effectively as “micro cylinders.” Such catalysts can dramatically improve physical surface area, for example per unit length of a reactor or reaction zone. At least a portion of the silica, originally present in the silica-containing fibers of a fibrous material used to form the fibrous substrate, is converted to a zeolite (e.g., having a SiO/AlOratio of at least about 150) that remains deposited on these fibers. The fibrous substrates possess important properties, for example in terms of acidity, which are useful in hydroprocessing (e.g., hydrotreating or hydrocracking) applications. 1. A catalyst comprising a fibrous substrate having silica-containing fibers and a zeolite , wherein the zeolite is present in the fibrous substrate in an amount of at least 20% by weight.2. The catalyst of claim 1 , wherein the zeolite is present in the fibrous substrate in an amount of at least 30% by weight.3. The catalyst of claim 1 , wherein the zeolite has a silica to alumina framework molar ratio of at least about 20.4. The catalyst of claim 3 , wherein the zeolite has an MFI structure type.5. The catalyst of claim 1 , wherein the zeolite has a Y claim 1 , beta claim 1 , or mordenite structure type.6. The catalyst of claim 1 , wherein the zeolite has framework silica derived from the silica-containing fibers.7. The catalyst of claim 6 , wherein the zeolite has framework silica derived from the silica-containing fibers and an additional silica source.8. The catalyst of claim 1 , wherein the zeolite has framework silica and alumina derived from the silica-containing fibers.9. The catalyst of claim 1 , wherein the silica-containing fibers are woven.10. The catalyst of claim 9 , wherein the fibrous substrate is in the form of a woven textile.11. A method of making a catalyst comprising contacting a fibrous material having silica- ...

CHA-type Zeolite Materials and Methods for Their Preparation Using Cycloalkyammonium Compounds

Aspects of the present invention relate to a process for the preparation of a zeolitic material having a CHA-type framework structure comprising YOand XO, wherein said process comprises the steps of: 1. A process for the preparation of a zeolitic material having a CHA-type framework structure comprising YOand XO , wherein said process comprises the steps of:{'sub': 2', '2', '3, 'sup': 1', '2', '3', '4', '+, '(1) providing a mixture comprising one or more sources for YO, one or more sources for XO, and one or more tetraalkylammonium cation RRRRN-containing compounds as structure directing agent;'}(2) crystallizing the mixture obtained in step (1) for obtaining a zeolitic material having a CHA-type framework structure;wherein Y is a tetravalent element and X is a trivalent element,{'sup': 1', '2', '3, 'wherein R, R, and Rindependently from one another stand for alkyl,'}{'sup': '4', 'wherein Rstands for cycloalkyl, and'}{'sub': 2', '5, 'wherein the mixture provided in step (1) does not contain any substantial amount of a source for ZO, wherein Z is P.'}2. The process of claim 1 , wherein R claim 1 , R claim 1 , and Rindependently from one another stand for optionally substituted and/or optionally branched (C-C)alkyl.3. The process of claim 1 , wherein Rstands for optionally heterocyclic and/or optionally substituted 5- to 8-membered cycloalkyl.4. The process of claim 1 , wherein the one or more tetraalkylammonium cation RRRRN-containing compounds comprise one or more N claim 1 ,N claim 1 ,N-tri(C-C)alkyl-(C-C)cycloalkylammonium compounds.5. The process of claim 1 , wherein the one or more tetraalkylammonium cation RRRRN-containing compounds are salts.6. The process of claim 1 , wherein Y is selected from the group consisting of Si claim 1 , Sn claim 1 , Ti claim 1 , Zr claim 1 , Ge claim 1 , and mixtures of two or more thereof.7. The process of claim 1 , wherein the one or more sources for YOcomprises one or more compounds selected from the group consisting of fumed ...

Hydrocarbon Conversion Process Using a High Throughpout Process for Manufacturing Molecular Sieves

A method of crystallizing a crystalline molecular sieve having a pore size in the range of from about 2 to about 19 Å, said method comprising the steps of (a) providing a mixture comprising at least one source of ions of tetravalent element (Y), at least one hydroxide source (OH − ), and water, said mixture having a solid-content in the range of from about 15 wt. % to about 50 wt. %; and (b) treating said mixture to form the desired crystalline molecular sieve with stirring at crystallization conditions sufficient to obtain a weight hourly throughput from about 0.005 to about 1 hr −1 , wherein said crystallization conditions comprise a temperature in the range of from about 200° C. to about 500° C. and a crystallization time less than 100 hr.

Oxidation catalyst for a lean burn internal combustion engine

An apparatus is disclosed. The apparatus comprises a lean-burn internal combustion engine, engine management means and an exhaust system for treating exhaust gas of the engine. The exhaust system comprises a first oxidation catalyst disposed on a first honeycomb monolith substrate. The first oxidation catalyst comprises platinum supported on a first metal oxide support comprising at least one reducible oxide, and is substantially free of alkali metals and alkaline earth metals. The engine management means is arranged, when in use, intermittently to modulate the lambda composition of the exhaust gas entering the first oxidation catalyst to a rich lambda composition.

PROCESS FOR THE CONVERSION OF OXYGENATES TO OLEFINS

The present invention relates to a process for converting oxygenates to olefins, comprising 126-. (canceled)27. A catalyst for the conversion of oxygenates to olefins , wherein the catalyst comprises one or more zeolites of the MFI , MEL and/or MWW structure type and particles of one or more metal oxides , the one or more zeolites of the MFI , MEL and/or MWW structure type comprising one or more alkaline earth metals , and the particles of the one or more metal oxides comprising phosphorus , the phosphorus being present at least partly in oxidic form , and the one or more alkaline earth metals being selected from the group consisting of Mg , Ca , Sr , Ba and combinations of two or more thereof.28. The catalyst according to claim 27 , wherein the one or more zeolites of the MFI claim 27 , MEL and/or MWW structure type comprise phosphorus claim 27 , the phosphorus being present at least partly in oxidic form.29. The catalyst according to claim 27 , wherein the one or more zeolites are of the MFI structure type.30. The catalyst according to claim 27 , wherein the alkaline earth metal is Mg.31. The catalyst according to claim 27 , wherein the one or more zeolites of the MFI claim 27 , MEL and/or MWW structure type comprise the one or more alkaline earth metals in a total amount in the range from 0.1 to 20% by weight claim 27 , based on the total amount of the one or more zeolites of the MFI claim 27 , MEL and/or MWW structure type and calculated as the metal.32. The catalyst according to claim 27 , wherein the one or more metal oxides are selected from the group consisting of alumina claim 27 , titania claim 27 , zirconia claim 27 , aluminum-titanium mixed oxides claim 27 , aluminum-zirconium mixed oxides claim 27 , aluminum-lanthanum mixed oxides claim 27 , aluminum-zirconium-lanthanum mixed oxides claim 27 , titanium-zirconium mixed oxides and mixtures of two or more thereof.33. The catalyst according to claim 27 , wherein the zeolite:metal oxide weight ratio in the ...

Synthesis and Use of M41S Family Molecular Sieves

A process is described for producing an M41S family molecular sieve. The process comprises preparing a synthesis mixture capable of forming said molecular sieve in a reactor, which is equipped with a mixer having a Froude number of at least 1, said synthesis mixture having a solids content of at least 20 wt %. The synthesis mixture is heated in the reactor while agitating the mixture with said mixer to form a product mixture comprising water and crystals of said molecular sieve material. Thereafter at least part of the water is removed from the product mixture in the reactor so as to decrease the water content of the product mixture inside the reactor by at least 5 wt %. 1. A process for producing a molecular sieve material having an X-ray diffraction pattern with at least one peak at a position greater than about 18 Angstrom Units d-spacing with a relative intensity of 100 , and a benzene adsorption capacity of greater than about 15 grams benzene per 100 grams anhydrous crystal at 50 torr and 25° C. , said process comprising the steps of:{'sub': 1', '2', '3', '4', '1', '2', '3', '4', '1', '2', '3', '4, 'sup': '+', '(a) preparing a synthesis mixture capable of forming said molecular sieve material by combining in a reactor equipped with a mixer having a Froude number of at least 1, at least water, a source of at least one oxide selected from the group consisting of divalent element W, trivalent element X, tetravalent element Y and pentavalent element Z, a source of an alkali or alkaline earth metal M, and an organic directing agent (R) having the formula RRRRQ, wherein Q is nitrogen or phosphorus and wherein at least one of R, R, Rand Ris selected from the group consisting of aryl of from 6 to about 36 carbon atoms, alkyl of from 6 to about 36 carbon atoms and combinations thereof and the remainder of R, R, Rand Ris selected from the group consisting of hydrogen, alkyl of from 1 to 5 carbon atoms and combinations thereof, said synthesis mixture having a solids ...

ISOMERISATION CATALYST PREPARATION PROCESS

A process for preparing an alkylaromatics isomerisation catalyst comprising at least 0.01% wt of platinum on a carrier comprising of from 1 to 9 wt % of ZSM-12 and inorganic binder, which process comprises treating the carrier with an impregnation solution comprising base and an anionic platinum complex which impregnation solution has a pH of from 5.5 to 8; and a process for the isomerisation of alkylaromatics with the help of catalyst thus obtained. 1. A process for preparing an alkylaromatics isomerisation catalyst comprising at least 0.01% wt of platinum on a carrier comprising of from 1 to 9 wt % of ZSM-12 and inorganic binder , which process comprises treating the carrier with an impregnation solution comprising base and an anionic platinum complex which impregnation solution has a pH of from 5.5 to 8.2. A process as claimed in in which the base is a compound according to the formula (RRRNH)OH in which the compounds R claim 1 , R claim 1 , Reach independently are chosen from the group consisting of hydrogen and alkyl containing of from 1 to 6 carbon atoms.3. A process as claimed in in which the impregnation is carried out by contacting the carrier with an excess of impregnation solution while stirring.4. A process as claimed in in which the impregnated carrier is dried and calcined at a temperature of from 300 to 600° C.5. A process as claimed in in which the silica to alumina molar ratio of the ZSM-12 is in the range of from 60 to 200.6. A process as claimed in in which the anionic platinum complex is a platinum chloride.7. A process for the isomerisation of alkylaromatics which process comprises contacting a hydrocarbon stream comprising alkylaromatics with a catalyst obtained in a process as claimed in . This invention relates to a zeolite-based catalyst for the isomerisation of alkylaromatics, more specifically ethylbenzene.Following fractionation or distillation of crude petroleum oil, a straight-run naphtha fraction is obtained. This fraction generally ...

PROCESS FOR TREATING SHAPED CATALYST BODIES AND SHAPED CATALYST BODIES HAVING INCREASED MECHANICAL STRENGTH

The present invention provides a process for treating shaped catalyst bodies which has the following steps: 116-. (canceled)17. A process for treating shaped catalyst bodies , which comprises the process steps:a) providing finished shaped catalyst bodies,b) impregnating the finished shaped catalyst bodies with a peptizing auxiliary in an amount of liquid which does not exceed the theoretical water absorption of the shaped catalyst bodies,c) thermal treating the impregnated shaped catalyst bodies at from 50° C. to 250° C. andd) calcinating the thermally treated shaped catalyst bodies at from 250° C. to 600° C.18. The process according to claim 17 , wherein an ammonia solution or a nitric acid solution is used as peptizing auxiliary.19. The process according to claim 18 , wherein an aqueous ammonia solution or an aqueous nitric acid solution is used as peptizing auxiliary.20. The process according to claim 17 , which claim 17 , after process step b) claim 17 , further comprises the process stepbb) allowing the peptizing auxiliary to act for up to 10 hours.21. The process according to claim 17 , wherein the thermal treatment in process step c) is carried out under atmospheric pressure or under reduced pressure or in a static or agitated bed of the shaped catalyst bodies.22. The process according to claim 21 , wherein the reduced pressure is from 0.1 to 0.9 bar.23. The process according to claim 17 , wherein the calcination in process step d) is carried out in a static or agitated bed of the shaped catalyst bodies.24. The process according to claim 17 , wherein extrudates or pellets or granules are used as shaped catalyst bodies.25. The process according to claim 17 , wherein heterogeneous catalysts are used as catalyst for the shaped catalyst bodies.26. The process according to claim 17 , wherein the catalyst is zeolite claim 17 , NiO/CoO/CuO/ZrO claim 17 , TiO claim 17 , CuO/AlOor CoO/SiO.27. The process according to claim 26 , wherein the zeolite is a boron-beta- ...

MOLECULAR SIEVES AND RELATED METHODS AND STRUCTURE DIRECTING AGENTS

Method for preparing molecular sieves and molecular sieves obtained thereby are described. The method includes preparing a reaction mixture, comprising a structure directing agent, at least one source of at least one oxide of a tetravalent element, optionally, one or more sources of one or more oxides selected from the group consisting of oxides of trivalent elements, pentavalent elements, and mixtures thereof, optionally, at least one source of an element selected from Groups 1 and 2 of the Periodic Table; and optionally, hydroxide ions or fluoride ions, and maintaining the reaction mixture under conditions sufficient to form crystals of the molecular sieve. In the method, various imidazolium cations are used as the structure directing element. 5. The method of claim 2 , wherein an imidazolium cation is associated with an anion selected from the group consisting of hydroxide claim 2 , fluoride claim 2 , chloride claim 2 , bromide claim 2 , iodide claim 2 , acetate claim 2 , sulfate claim 2 , tetrafluoroborate and carboxylate.6. The method of claim 1 , wherein the tetravalent element is selected from the group consisting of silicon claim 1 , germanium and titanium.7. The method of claim 1 , wherein the tetravalent element is silicon.8. The method of claim 1 , wherein the source of the tetravalent element is selected from the group consisting of oxides claim 1 , hydroxides claim 1 , acetates claim 1 , oxalates claim 1 , ammonium salts and sulfates of the tetravalent element.9. The method of claim 1 , wherein the source of an element selected from Groups 1 and 2 of the Periodic Table is selected from the group consisting of an alkali metal hydroxide and an alkaline earth metal hydroxide.10. The method of claim 9 , wherein the alkali metal hydroxide is selected from the group consisting of sodium hydroxide claim 9 , potassium hydroxide claim 9 , lithium hydroxide claim 9 , cesium hydroxide and rubidium hydroxide.11. The method of claim 9 , wherein the alkaline earth ...

CATALYST FOR THE ALKYLATION OF AROMATIC HYDROCARBONS

The present invention relates to catalyst composition prepared by a method wherein an aluminosilicate zeolite having its pores filled with templating agent with a specific organic silicon compound to deposit said organic silicon compound on the surface of the zeolite to provide an organosilicon treated catalyst precursor; and calcining the organosilicon treated catalyst precursor under conditions sufficient to remove the templating agent from the zeolite. Furthermore, the present invention relates to a method for preparing said catalyst composition and a process for alkylation of an aromatic hydrocarbon comprising contacting the catalyst composition of the present invention with a feed stream comprising said aromatic hydrocarbon and an alkylating agent under aromatic alkylation conditions. 2. The method according to claim 1 , wherein the alkyl disilazane is selected from the group consisting of hexamethyldisilazane and hexaethyldisilazane.3. The method according to claim 1 , wherein the alkoxy silane is selected from the group consisting of methoxytrimethylsilane claim 1 , ethoxytrimethylsilane claim 1 , propoxytrimethylsilane claim 1 , methyltrimethoxysilane claim 1 , methyltriethoxysilane claim 1 , ethyltrimethoxysilane claim 1 , ethyltriethoxysilane claim 1 , propyltrimethoxysilane and propyltriethoxysilane.4. The method according to claim 1 , wherein the halo alkyl silane is selected from the group consisting of dichlorodimethylsilane and dichlorodiethylsilane.5. The method according to claim 1 , wherein the zeolite is a large pore size aluminosilicate zeolite.6. The method according to claim 1 , wherein the zeolite is calcined in step (b) at a temperature of 450-600° C. for 3-8 hrs in an oxygen comprising atmosphere.7. The method according to claim 1 , wherein the zeolite is washed in organic solvent before the calcination step (b) is performed.8. A catalyst composition obtainable by the method according to .9. A process for alkylation of an aromatic ...

Low pressure transalkylation process

A process for transalkylation is described. The process operates at a lower pressure than a typical transalkylation processes, and provides higher benzene purity with comparable or lower ring loss compared to the typical transalkylation process. The xylene selectivity is comparable to or higher than the standard process, and the ethyl benzene selectivity is comparable to or lower than the standard process.

CATALYTIC COMPOSITION WITH ADDED COPPER TRAPPING COMPONENT FOR NOx ABATEMENT

The present disclosure provides catalyst compositions for NOx conversion and wall-flow filter substrates comprising such catalyst compositions. Certain catalyst compositions include a zeolite with sufficient Cu exchanged into cation sites thereof to give a Cu/Al ratio of 0.1 to 0.5 and a CuO loading of 1 to 15 wt. %; and a copper trapping component (e.g., alumina) including a plurality of particles having a D90 particle size of about 0.5 to 20 microns in a concentration of about 1 to 20 wt. %. The zeolite and copper trapping component can be in the same washcoat layer or can be in different washcoat layers (such that the copper trapping component serves as a “pre-coating” on the wall-flow filter substrate).

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

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

METHODS FOR PRODUCING MESOPOROUS ZEOLITE MULTIFUNCTIONAL CATALYSTS FOR UPGRADING PYROLYSIS OIL

A method of making a multifunctional catalyst for upgrading pyrolysis oil includes contacting a hierarchical mesoporous zeolite support with a solution including at least a first metal catalyst precursor and a second metal catalyst precursor, each or both of which may include a heteropolyacid. The hierarchical mesoporous zeolite support may have an average pore size of from 2 nm to 40 nm. Contacting the hierarchical mesoporous 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 hierarchical mesoporous zeolite support to produce a multifunctional catalyst precursor. The method further includes removing excess solution 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 hierarchical mesoporous zeolite support. 1. A method of making a multifunctional catalyst for upgrading pyrolysis oil , the method comprising: the hierarchical mesoporous zeolite support has an average pore size of from 2 nanometers to 40 nanometers as determined by Barrett-Joyner-Halenda (BJH) analysis;', 'the first metal catalyst precursor, the second metal catalyst precursor, or both, comprises a heteropolyacid having at least one heteroatom selected from the group consisting of phosphorous, silicon, germanium, arsenic, and combinations of these; and', 'the contacting deposits the first metal catalyst precursor and the second metal catalyst precursor onto outer surfaces and pore surfaces of the hierarchical mesoporous zeolite support to produce a multifunctional catalyst precursor;, 'contacting a hierarchical mesoporous zeolite support with a solution comprising at least a first metal catalyst precursor and a second metal catalyst precursor, whereremoving excess solution from the multifunctional catalyst precursor; ...

METHODS FOR PRODUCING MESOPOROUS ZEOLITE MULTIFUNCTIONAL CATALYSTS FOR UPGRADING PYROLYSIS OIL

A method of making a multifunctional catalyst for upgrading pyrolysis oil includes contacting a hierarchical mesoporous zeolite support with a solution including at least a first metal catalyst precursor and a second metal catalyst precursor, each or both of which may include a heteropolyacid. The hierarchical mesoporous zeolite support may have an average pore size of from 2 nm to 40 nm. Contacting the hierarchical mesoporous 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 hierarchical mesoporous zeolite support to produce a multifunctional catalyst precursor. The method further includes removing excess solution 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 hierarchical mesoporous zeolite support. 112-. (canceled)13. A multifunctional catalyst for upgrading pyrolysis oil produced by a method comprising: the hierarchical mesoporous zeolite support has an average pore size of from 2 nanometers to 40 nanometers as determined by Barrett-Joyner-Halenda (BJH) analysis;', 'the first metal catalyst precursor, the second metal catalyst precursor, or both, comprises a heteropolyacid; and', 'the contacting deposits the first metal catalyst precursor and the second metal catalyst precursor onto outer surfaces and pore surfaces of the hierarchical mesoporous zeolite support to produce a multifunctional catalyst precursor;, 'contacting a hierarchical mesoporous zeolite support with a solution comprising at least a first metal catalyst precursor and a second metal catalyst precursor, whereremoving excess solution from the multifunctional catalyst precursor; andcalcining the multifunctional catalyst precursor to produce the multifunctional catalyst comprising at least a first metal 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 ...

Exhaust gas purifying catalyst and exhaust gas purification method using same

A catalyst that is not only capable of efficiently treating CO even at a low exhaust gas temperature, but also capable of exerting favorable CO purification efficiency in a low-temperature exhaust gas even in a case of being exposed for a long time to an engine exhaust gas that is a high temperature and contains HC, CO, NOx, water vapor and the like; and an exhaust gas treatment technique are described. The catalyst for purifying exhaust gas contains: a noble metal; an oxide containing as a base material A at least two kinds of elements selected from the group consisting of aluminum, zirconium and titanium; and an oxide containing as a base material B at least one kind of element selected from the group consisting of silicon, cerium, praseodymium and lanthanum; in which the base material A and the base material B satisfy a specific formula.

Process for Making Alkylated Aromatic Compound

A process for producing an alkylated aromatic compound comprises contacting an aromatic starting material and hydrogen with a plurality of catalyst particles under hydroalkylation conditions to produce an effluent comprising the alkylated aromatic compound, the catalyst comprising a composite of a solid acid, an inorganic oxide different from the solid acid and a hydrogenation metal, wherein the distribution of the hydrogenation metal in at least 60 wt % of the catalyst particles is such that the average concentration of the hydrogenation metal in the rim portion of a given catalyst particle is Crim, the average concentration of the hydrogenation metal in the center portion of the given catalyst particle is Ccenter, where 0.2≦Crim/Ccenter<2.0. Also disclosed are hydroalkylation catalyst and process for making phenol and/or cyclohexanone using the catalyst.

CLUSTER SUPPORTED CATALYST AND PRODUCTION METHOD THEREFOR

A method for producing a cluster-supporting catalyst, the cluster-supporting catalyst including porous carrier particles that has acid sites, and catalyst metal clusters supported within the pores of the porous carrier particles, includes the following steps: providing a dispersion liquid containing a dispersion medium and the porous carrier particles dispersed in the dispersion medium; and in the dispersion liquid, forming catalyst metal clusters having a positive charge, and supporting the catalyst metal clusters on the acid sites within the pores of the porous carrier particles through an electrostatic interaction. 1. A method for producing a cluster-supporting catalyst ,wherein the cluster-supporting catalyst comprises porous carrier particles having acid sites, and catalyst metal clusters supported within the pores of the porous carrier particles; andwherein the method comprises the followings steps:providing a dispersion liquid containing a dispersion medium and the porous carrier particles dispersed in the dispersion medium, andforming, in the dispersion liquid, catalyst metal clusters having a positive charge, and supporting the catalyst metal clusters on the acid sites within the pores of the porous carrier particles through an electrostatic interaction.2. The method according to claim 1 , wherein the dispersion liquid is provided by pulverizing the porous carrier particles claim 1 , and dispersing the pulverized porous carrier particles in the dispersion medium.3. The method according to claim 1 , wherein the clusters are formed in the dispersion liquid by any of the following methods:a method of laser ablation in liquid,a method of microwave ablation in liquid,a method of plasma ablation in liquid, anda positive-negative inversion method.4. The method according to claim 1 , wherein the clusters are formed in the dispersion liquid by a method of reduction in liquid.5. The method according to claim 4 , wherein the dispersion liquid is irradiated with plasma ...

MOLECULAR SIEVE SSZ-95, METHOD OF MAKING, AND USE

A new crystalline molecular sieve designated SSZ-95 is disclosed. In general, SSZ-95 is synthesized from a reaction mixture suitable for synthesizing MTT-type molecular sieves and maintaining the mixture under crystallization conditions sufficient to form product. The product molecular sieve is subjected to a pre-calcination step, and ion-exchange to remove extra-framework cations, and a post-calcination step. The molecular sieve has a MTT-type framework and a H-D exchangeable acid site density of 0 to 50% relative to molecular sieve SSZ-32. 1. A molecular sieve having a MTT-type framework , a mole ratio of 20 to 70 of silicon oxide to aluminum oxide , a total micropore volume of between 0.005 and 0.02 cc/g; and a H-D exchangeable acid site density of up to 50% relative to SSZ-32.2. The molecular sieve of claim 1 , wherein the molecular sieve has a mole ratio of 20 to 50 of silicon oxide to aluminum oxide.3. The molecular sieve of claim 1 , wherein the molecular sieve has a total micropore volume of between 0.008 and 0.018 cc/g.4. The molecular sieve of claim 1 , wherein the molecular sieve has an external surface area of between 200 and 250 m/g; and a BET surface area of between 240 and 280 m/g.5. The molecular sieve of claim 1 , wherein the molecular sieve has a H-D exchangeable acid site density of 0.5 to 30% relative to molecular sieve SSZ-32.6. The molecular sieve of claim 5 , wherein the molecular sieve has a total micropore volume of between 0.008 and 0.018 cc/g.7. The molecular sieve of claim 5 , wherein the molecular sieve has an external surface area of between 200 and 250 m/g; and a BET surface area of between 240 and 280 m/g.8. The molecular sieve of claim 1 , wherein the molecular sieve has a H-D exchangeable acid site density of 2 to 25% relative to molecular sieve SSZ-32.9. The molecular sieve of claim 8 , wherein the molecular sieve has a total micropore volume of between 0.008 and 0.018 cc/g.10. The molecular sieve of claim 8 , wherein the molecular ...

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

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

CATALYST, AND METHOD FOR DIRECT CONVERSION OF SYNGAS TO PREPARE LIGHT OLEFINS

A process for direct synthesis of light olefins uses syngas as the feed raw material. This catalytic conversion process is conducted in a fixed bed or a moving bed using a composite catalyst containing components A and B (A+B). The active ingredient of catalyst A is metal oxide; and catalyst B is an oxide supported zeolite. A carrier is one or more of AlO, SiO, TiO, ZrO, CeO, MgO and GaOhaving hierarchical pores; the zeolite is one or more of CHA and AEI structures. The loading of the zeolite is 4%-45% wt. A weight ratio of the active ingredients in the catalyst A and the catalyst B is within a range of 0.1-20, and preferably 0.3-5. The total selectivity of the light olefins comprising ethylene, propylene and butylene can reach 50-90%, while the selectivity of a methane byproduct is less than 15%. 1. A catalyst , wherein the catalyst is a composite catalyst composed of A+B; the catalyst component A and the catalyst component B are compounded by mechanical mixing method; the active ingredients of the catalyst component A are active metal oxides; the catalyst component B are supported zeolites; the carrier is at least one of porous AlO , SiO , TiO , ZrO , CeO , MgO and GaO; the zeolite is at least one of CHA and AEI structures; the loading of the zeolite is 4%-45% wt; and the active metal oxide is at least one of MnO , MnCrO , MnAlO , MnZrO , ZnO , ZnCrO , ZnAlO , CoAlOand FeAlO.2. The catalyst according to claim 1 , wherein at least one of porous AlO claim 1 , SiO claim 1 , TiO claim 1 , ZrO claim 1 , CeO claim 1 , MgO and GaOin the catalyst component B is used as the carrier; specific surface area is 30-250 m/g; pore volume is 0.25-0.80 ml/g; through calculation according to the specific surface area claim 1 , mesoporous specific surface area occupies 30-75% and macroporous specific surface area occupies 25-70%; and the zeolite is used as an active component and dispersed on the carrier by in situ growth or physical mixing mode.3. The catalyst according to claim 1 , ...

MOLECULAR SIEVE, MANUFACTURING METHOD THEREFOR, AND USES THEREOF

This invention relates to a molecular sieve, which has a specific XRD diffraction pattern and a specific layered structure. As compared with a prior art molecular sieve, the molecular sieve according to this invention exhibits improved catalytic performances and good service life and regeneration performance. The molecular sieve can be produced with a simplified procedure, under mild operation conditions, with less energy and material consumption and less side reactions, with a high product purity at low cost and a high yield. The molecular sieve according to this invention is especially suitable for use as an adsorbent or a catalyst. 5. The molecular sieve according to or , wherein the total pore volume (by the BET method) is not less than 0.5 cm/g , preferably 0.55-0.90 cm/g , the total specific surface area (by the BET method) is not less than 450 m/g , preferably 480-680 m/g , the external specific surface area (by the BET method) is not less than 185 m/g , preferably 200-400 m/g , and the external specific surface area accounts for not less than 40% , preferably 45-65% of the total specific surface area.6. The molecular sieve according to or , having a MWW topological framework structure , wherein at least 80% , preferably at least 85% , more preferably at least 90% , more preferably at least 95% , more preferably at least 99% of all crystals thereof are flake crystals having a thickness of about 5 nm by the TEM method.8. The process according to claim 7 , wherein the aza monocyclic cycloalkane has a C/N ratio of greater than 2 claim 7 , more preferably 2.5 or more claim 7 , the compound represented by the formula (I) has a C/N ratio of 10 or more claim 7 , 12 or more or 13 or more claim 7 , and the aza arene has a C/N ratio of 9 or more claim 7 , 10 or more or 11 or more.9. The process according to claim 7 , wherein the ratio by molar between the first oxide source (calculated as the first oxide) claim 7 , the second oxide source (calculated as the second ...

ZEOLITE SSZ-52x

The present invention relates to new crystalline zeolite SSZ-52prepared using a quaternary ammonium cation templating agent, for example, having the structure: 1. A zeolite having a mole ratio of 6-50 of an oxide selected from the group consisting of silicon oxide , germanium oxide and mixtures thereof to an oxide selected from aluminum oxide , gallium oxide , iron oxide and mixtures thereof , and exhibiting in the as synthesized form the XRD pattern of .2. A zeolite according to claim 1 , wherein the oxides comprise silicon oxide and aluminum oxide.3. A zeolite according to claim 1 , wherein said zeolite is in the hydrogen form.5. A zeolite according to claim 4 , wherein W is aluminum and Y is silicon.7. The method of claim 6 , wherein the MYOratio is in the range of 0.60-0.90.8. The method according to claim 6 , wherein the oxides are silicon oxide and aluminum oxide.9. The method of claim 6 , wherein the crystalline material has claim 6 , after calcination claim 6 , the X-ray diffraction lines of Table IV.10. The method of claim 6 , wherein the crystalline material exhibits a NOconversion of 100% at 250° C. after aging at 750° C. for 80 hr at 10% humidity.11. A product prepared by the process of .13. The method according to wherein the oxides are silicon oxide and aluminum oxide.14. The method of wherein the crystalline material has claim 12 , after calcination claim 12 , the X-ray diffraction lines of Table III.15. The method of claim 12 , wherein the crystalline material exhibits a NOconversion of 100% at 250° C. after aging at 750° C. for 80 hr at 10% humidity.16. The method of claim 12 , wherein the MYOratio is in the range of 0.60-0.90.17. A product prepared by the process of . The present invention relates to new crystalline zeolite SSZ-52x, a method for preparing SSZ-52x using a quaternary ammonium cation templating agent such as, for example, N,N-diethyl-5,8-dimethyl-2-azonium bicyclo[3.2.2]nonane, and processes employing SSZ-52x as a catalyst.Because of ...

MOLECULAR SIEVE SSZ-91, METHODS FOR PREPARING SSZ-91, AND USES FOR SSZ-91

A family of new crystalline molecular sieves designated SSZ-91 is disclosed, as are methods for making SSZ-91 and uses for SSZ-91. Molecular sieve SSZ-91 is structurally similar to sieves falling within the ZSM-48 family of molecular sieves, and is characterized as: (1) having a low degree of faulting, (2) a low aspect ratio that inhibits hydrocracking as compared to conventional ZSM-48 materials having an aspect ratio of greater than 8, and (3) is substantially phase pure. 1. A molecular sieve belonging to the ZSM-48 family of zeolites , wherein the molecular sieve comprises:a silicon oxide to aluminum oxide mole ratio of 40 to 200,at least 70% polytype 6 of the total ZSM-48-type material present in the product, andan additional EUO-type molecular sieve phase in an amount of between 0 and 3.5 percent by weight of the total product; andwherein the molecular sieve has a morphology characterized as polycrystalline aggregates comprising crystallites collectively having an average aspect ratio of between 1 and 8.3. The molecular sieve of or , wherein the molecular sieve has a silicon oxide to aluminum oxide mole ratio of 70 to 160.4. The molecular sieve of any of - , wherein the molecular sieve has a silicon oxide to aluminum oxide mole ratio of 80 to 140.5. The molecular sieve of any of - , wherein the molecular sieve comprises at least 80% polytype 6 of the total ZSM-48-type material present in the product.6. The molecular sieve of any of - , wherein the molecular sieve comprises between 0.1 and 2 wt. % EU-1.7. The molecular sieve of any of - , wherein the crystallites collectively have an average aspect ratio of between 1 and 5.8. The molecular sieve of any of - , wherein the molecular sieve comprises at least 90% polytype 6 of the total ZSM-48-type material present in the product.9. The molecular sieve of any of - , wherein the crystallites collectively have an average aspect ratio of between 1 and 3.10. A method of preparing a molecular sieve according to any of - ...

PROCESS FOR PREPARING AN UNSATURATED ALCOHOL

The present invention relates to a process for preparing an unsaturated alcohol, preferably 3,7-dimethyl-2,6-octadienal, by contacting an alkene, preferably isobutene, with formaldehyde in the presence a condensation catalyst comprising a zeolitic material comprising the framework structure of which comprises a tetravalent element Y other than Si. 115.-. (canceled)17. The process of claim 16 , wherein Y is one or more of Sn and Zr.18. The process of claim 16 , where the framework structure of the zeolitic material in (ii) comprises Y in an amount of from 1 to 20 weight-% claim 16 , based on the total weight of the zeolitic material.19. The process of claim 16 , wherein the framework structure of the zeolitic material in (ii) does not comprise a trivalent element X other than optionally Al.20. The process of claim 16 , wherein at least 99 weight-% of the framework structure of the zeolitic material in (ii) consist of Si claim 16 , Y claim 16 , O and H.21. The process of claim 16 , wherein the framework structure of the zeolitic material in (ii) has framework type BEA claim 16 , MFI claim 16 , MWW claim 16 , or a mixed structure thereof.22. The process of claim 21 , wherein the zeolitic material comprises Sn in an amount in the range of from 2 to 20 weight-% based on the total weight of the zeolitic material.23. The process of claim 16 , wherein the formaldehyde in (i) is one or more of aqueous formaldehyde claim 16 , trioxane and paraformaldehyde.24. The process of claim 16 , wherein in the mixture provided in (i) claim 16 , the molar ratio of the compound of formula (I) relative to the formaldehyde claim 16 , calculated as CHO claim 16 , is in the range from 1:1 to 12:1.25. The process of claim 16 , wherein the mixture in provided in (i) additionally comprises a solvent.26. The process of claim 16 , wherein the contacting in (ii) is effected at a temperature of the mixture in the range of from 60 to 150° C.27. The process of claim 16 , wherein the contacting in (ii) ...

PROCESS TO PREPARE PROPYLENE

The invention is directed to a process to prepare propylene from a hydrocarbon feedstock comprising olefin hydrocarbon compounds by contacting the feedstock with a mixture of a heterogeneous cracking catalyst and a heterogeneous dehydrogenation catalyst as present in one or more packed beds thereby obtaining propylene and other reaction products. 1. A process to prepare propylene(i) from a hydrocarbon feedstock comprising olefin hydrocarbon compounds by contacting the feedstock with a mixture of a heterogeneous cracking catalyst and a heterogeneous dehydrogenation catalyst as present in one or more packed beds thereby obtaining propylene and other reaction products, wherein the cracking catalyst and the dehydrogenation catalyst are present in one or more packed beds in an in-series configuration and wherein the hydrocarbon feedstock, formed propylene and other reaction products will flow from an up-flow region to a down-flow region following a flow path and wherein in the direction of the flow path the concentration of the dehydrogenation catalyst in the bed increases compared to the cracking catalyst and/or(ii) from a hydrocarbon feedstock comprising paraffinic hydrocarbon compounds by contacting the feedstock with a mixture of a heterogeneous cracking catalyst and a heterogeneous dehydrogenation catalyst as present in one or more packed beds thereby obtaining propylene and other reaction products, wherein the cracking catalyst and the dehydrogenation catalyst are present in one or more packed beds in an in-series configuration and wherein the hydrocarbon feedstock, formed propylene and other reaction products will flow from an up-flow region to a down-flow region following a flow path and wherein in the direction of the flow path the concentration of the dehydrogenation catalyst in the bed decreases compared to the cracking catalyst.2. The process according to claim 1 , wherein the content of olefins having 4 or more carbon atoms in the feedstock of process (i) is ...

Molecular sieves with a linde type a topology and related methods and systems

A method for preparing molecular sieves with a Linde Type A (LTA) topology structure, and molecular sieves obtained thereby are described wherein a structure directing agent comprising a triquaternary cation is contacted with a source of a first oxide of a first tetravalent element or a source of a first oxide of a trivalent element; and a source of an oxide of a pentavalent elements.

Method for preparing fructose or xylulose from biomass containing glucose or xylose using butanol, and method for separating the same

The present invention relates to a method for preparing fructose or xylulose from biomass comprising glucose or xylose, and a method for separating a mixture of glucose and fructose and a mixture of xylose and xylulose.

DUAL PHASE CATALYSTS SYSTEM FOR MIXED OLEFIN HYDRATIONS

The catalyst systems include a dual phase catalyst system that includes a water soluble acid catalyst and a solid acid catalyst. 2. The system of where the water soluble acid comprises an organic acid selected from the group consisting of acetal acid claim 1 , tosylate acid claim 1 , perflurated acetic acid claim 1 , lactic acid claim 1 , citric acid claim 1 , oxalic acid claim 1 , benzoic acid claim 1 , and combinations thereof.3. The system of where the water soluble acid comprises an inorganic acid selected from the group consisting of HCl claim 1 , HPO claim 1 , HSO claim 1 , hydrofluric acid claim 1 , heteropoly acids claim 1 , and combinations thereof.4. The system of where the solid acid catalyst is selected from the group consisting of an ionic exchange resin claim 1 , a zeolite claim 1 , a supported acid claim 1 , and combinations thereof.5. The system of where the mixed olefins are selected from the group consisting of propylene claim 1 , n-butene claim 1 , 2-butene claim 1 , isobutene claim 1 , pentenes claim 1 , hexenes claim 1 , olefins having more than 6 carbons claim 1 , and combinations thereof.6. The system of where the conversion rate for the dual phase catalyst system is equal to or greater than about 10%.7. The system of where the dual phase catalyst system is capable of converting the mixed olefins into the mixed alcohols having a ratio of 2-butanol to t-butanol that is greater than either the ratio of 2-butanol to t-butanol of the water soluble acid catalyst or the ratio of 2-butanol to t-butanol of the solid acid catalyst claim 1 , and where the mixed olefins comprise butenes.8. The system of where the ratio of 2-butanol to t-butanol for the dual phase catalyst system is equal to or greater than about 2.0. This application is a continuation of U.S. patent application Ser. No. 12/946,014, filed Nov. 15, 2010, now U.S. Pat. No. 8,558,036, and a divisional application of U.S. patent application Ser. No. 14/025,318, filed Sep. 12, 2013. For ...

Honeycomb structural body

A honeycomb structural body has plural cell density sections having a cell density which is changed stepwise in a radial direction. A partition wall is formed between adjacent cell density sections. The cell density sections have a high cell density section having a maximum cell density, excepting an outermost cell density section formed at an outermost side, and a low cell density section having a minimum cell density, excepting an innermost cell density section formed at an innermost side. A relationship of V−Va≧Vb+Vs is satisfied, where V indicates a volume of the honeycomb structural body if the overall honeycomb structural body is composed of the high cell density section, Va indicates a volume of the high cell density section, Vb indicates a volume of the cell density section, and Vs indicates a volume of the boundary wall which separates the low cell density section from the cell density section formed immediately inside of the low cell density section.

MICROWAVE CATALYST AND PREPARATION PROCESS AND USE THEREOF

Provided is a microwave catalyst. The microwave catalyst comprises: i) an active catalyst component comprising a metal and/or a metal oxide; ii) a microwave-absorbing component comprising at least one of CuO, ferrite spinel, and active carbon; and iii) a support. The microwave catalyst can be used for denitration by microwave catalysis, and has advantages such as high denitration efficiency, low energy consumption, environmental friendliness, and low costs. Also provided is a process for preparing the microwave catalyst and the use thereof. 1. A microwave catalyst , comprising:i) an active catalyst component, comprising a metal and/or a metal oxide;ii) a microwave-absorbing component, comprising at least one of CuO, ferrite spinel, and active carbon; andiii) a support.2. The microwave catalyst according to claim 1 , wherein the metal is at least one selected from the group consisting of Cu claim 1 , Mn claim 1 , Ce claim 1 , Ti claim 1 , V claim 1 , Mg claim 1 , and Fe claim 1 , preferably Cu; and the metal oxide is at least one oxide selected from the oxides of Cu claim 1 , Mn claim 1 , Ce claim 1 , Ti claim 1 , V claim 1 , Mg claim 1 , and Fe claim 1 , preferably CuO.3. The microwave catalyst according to claim 1 , wherein the support has a porous structure capable of absorbing microwave claim 1 , preferably being active carbon and/or a molecular sieve.4. The microwave catalyst according to claim 3 , wherein the molecular sieve is a ZSM-type molecular sieve claim 3 , Y-type molecular sieve claim 3 , or 13-type molecular sieve claim 3 , preferably a ZSM-5 molecular sieve.5. The microwave catalyst according to claim 1 , wherein the catalyst preferably contains Cu-ZSM-5 or Cu—Y.6. The microwave catalyst according to claim 5 , wherein the content of Cu in Cu-ZSM-5 is in the range from 2% to 12% by mass.7. The microwave catalyst according to claim 5 , wherein the content of Cu in Cu—Y is in the range from 2% to 15% by mass.8. The microwave catalyst according to claim 1 ...

MFI ZEOLITE HAVING UNIFORM MESOPORES AND METHOD FOR PRODUCING SAME

A novel MFI zeolite that when used as a catalyst, can be used for a selective catalytic reaction for larger molecules and provides a method for producing the MFI zeolite. The MFI zeolite includes uniform mesopores having a pore distribution curve which a peak-width thereof at half height (hw) is at most 20 nm (hw≦20 nm) and a center value (μ) of a maximum peak is 10 nm or more and 20 nm or less (10 nm≦μ≦20 nm), and having a pore volume (pv) of the uniform mesopores of at least 0.05 mL/g (0.05 mL/g≦pv); the MFI zeolite has no peak in a range of 0.1° to 3° in powder X-ray diffraction measurement with a diffraction angle represented by 2θ; and the MFI zeolite has an average particle diameter (PD) of at most 100 nm (PD≦100 nm). 1. An MFI zeolite comprising the following properties:(i) the MFI zeolite includes uniform mesopores having a pore distribution curve which a peak-width thereof at half height (hw) is at most 20 nm (hw≦20 nm) and a center value (μ) of a maximum peak is 10 nm or more and 20 nm or less (10 nm≦μ≦20 nm), and having a pore volume (pv) of the uniform mesopores of at least 0.05 mL/g (0.05 mL/g≦pv);(ii) the MFI zeolite has no peak in a range of 0.1° to 3° in powder X-ray diffraction measurement with a diffraction angle represented by 2θ; and(iii) the MFI zeolite has an average particle diameter (PD) of at most 100 nm (PD≦100 nm).2. The MFI zeolite according to claim 1 , wherein the peak-width at half height (hw) is 10 nm or less (hw≦10 nm).3. The MFI zeolite according to claim 1 , wherein a ratio (pvr) of the pore volume of the uniform mesopores having the properties shown in (i) with respect to a total pore volume of mesopores is 30% or more and 100% or less (30%≦pvr≦100%).4. The MFI zeolite according to claim 1 , wherein an SiO/AlOmolar ratio is 20 or more and 200 or less (20≦SiO/AlOmolar ratio≦200).5. A method for producing the MFI zeolite according to claim 1 , the method comprising subjecting a raw material composition having the following chemical ...

Separation, Storage, and Catalytic Conversion of Fluids Using ITQ-55

This invention refers to a microporous crystalline material of zeolitic nature that has, in its calcined state and in the absence of defects in its crystalline matrix manifested by the presence of silanols, the empirical formula 2. The method of claim 1 , wherein the zeolite ITQ-55 has claim 1 , in a calcined state and in an absence of defects in its crystalline matrix manifested by the presence of silanols claim 1 , an empiric formula{'br': None, 'i': x', 'y', ':g', '−g, 'sub': 1/n', '2', '2', '2', '2, '(MXO):YOGeO:(1)SiO'}in which{'sup': '+', 'M is selected between H, at least one inorganic cation of charge +n, and a mixture of both,'}X is at least one chemical element of oxidation state +3,Y is at least one chemical element with oxidation state +4 different from Si,x takes a value between 0 and 0.2, both included,y takes a value between 0 and 0.1, both included,g takes a value between 0 and 0.5, both included.3. The method of claim 2 , wherein x takes a value of essentially zero claim 2 , y takes a value of essentially zero claim 2 , and g takes a value of essentially zero.4. The method of claim 2 , wherein X is selected from Al claim 2 , Ga claim 2 , B claim 2 , Fe claim 2 , Cr claim 2 , and combinations thereof claim 2 , y takes the value 0 claim 2 , and g takes the value 0.5. The method of claim 4 , wherein the zeolite ITQ-55 comprises Si claim 4 , O claim 4 , and Al.6. The method of claim 5 , wherein a ratio of Si to Al is from about 10:1 to about 1000:1.7. The method of claim 6 , wherein the ratio of Si to Al is at least about 100:1.8. The method of claim 1 , wherein exposing the input fluid stream to the catalyst comprising zeolite ITQ-55 comprises exposing the input fluid stream to catalyst particles comprising zeolite ITQ-55.9. The method of claim 8 , wherein the input fluid stream is exposed to the catalyst particles comprising zeolite ITQ-55 in a fluidized bed reactor or a riser reactor.10. The method of claim 8 , wherein the catalyst particles ...

METHODS FOR PREPARATION OF CHA ZEOLITE AT AMBIENT PRESSURE

The disclosure, in one aspect, relates to methods of preparing a CHA zeolite under ambient pressure conditions. In further aspects, the disclosure relates to methods such that a mother liquor can be isolated from a disclosed method, and recycled for use in a disclosed method for further preparation of a CHA zeolite. This abstract is intended as a scanning tool for purposes of searching in the particular art and is not intended to be limiting of the present disclosure. 1. A method for preparing a CHA zeolite , the method comprising:heating a zeolite precursor mixture at ambient pressure in a reflux reaction vessel of a reflux reactor system comprising the reflux reaction vessel and a reflux condenser;wherein the zeolite precursor mixture comprises water, a silicate solution, a zeolite, and a CHA templating agent;wherein heating comprises heating the reaction vessel such the zeolite precursor mixture in the reflux reaction vessel has a reaction temperature of from about 80° C. to about 120° C.;thereby forming a CHA zeolite and a mother liquor solution.2. The method of claim 1 , wherein the ambient pressure is about 700 torr to about 800 torr.3. The method of claim 1 , wherein the zeolite in the zeolite precursor mixture is selected from a USY zeolite claim 1 , a pre-treated Na-Y zeolite claim 1 , a Na-Y zeolite claim 1 , and combinations thereof.4. The method of claim 3 , wherein the zeolite in the zeolite precursor mixture is selected from a pre-treated Na-Y zeolite claim 3 , a Na-Y zeolite claim 3 , and combinations thereof.5. The method of claim 3 , wherein the zeolite in the zeolite precursor mixture is a USY zeolite.6. The method of claim 1 , wherein the silicate in the zeolite precursor mixture is a sodium silicate solution comprising SiO claim 1 , NaO claim 1 , and water.7. The method of claim 1 , wherein the CHA templating agent is selected from N claim 1 ,N claim 1 ,N-trimethyl-1-ammonium adamantine claim 1 , tetraethylenepentamine claim 1 , and a combination ...

METHODS FOR PRODUCING HIERARCHICAL MESOPOROUS BETA ZEOLITE

A method for producing a hierarchical mesoporous beta includes mixing a beta zeolite with an aqueous metal hydroxide solution and heating the beta zeolite and the aqueous metal hydroxide mixture to produce a desilicated beta zeolite, contacting the desilicated beta zeolite with an ammonium salt solution to produce an intermediate hierarchical mesoporous beta zeolite, and treating the intermediate hierarchical mesoporous beta zeolite with an acidic solution to produce the hierarchical mesoporous beta zeolite. The hierarchical mesoporous beta zeolite includes a molar ratio of silicon to aluminum of greater than 12.5, a total pore volume of greater than or equal to the total pore volume of the intermediate hierarchical mesoporous beta zeolite, and an average mesopore size of greater than or equal to the average mesopore size of the hierarchical mesoporous beta zeolite. The method may also include calcining the intermediate hierarchical mesoporous beta zeolite. 1. A method for producing a hierarchical mesoporous beta zeolite , the method comprising:mixing a beta zeolite with an aqueous metal hydroxide solution;heating the beta zeolite and the aqueous metal hydroxide mixture at a temperature of greater than or equal to 100° C., wherein the heating causes desilication of the beta zeolite to produce a desilicated beta zeolite;{'sup': '3', 'contacting the desilicated beta zeolite with an ammonium salt solution to produce an intermediate hierarchical mesoporous beta zeolite comprising (a) a molar ratio of silicon to aluminum of less than 12.5, (b) a total pore volume of greater than or equal to 0.3 cm/g, and (c) an average mesopore size of greater than 8 nm, wherein the contacting causes ion exchange of sodium ions with ammonium ions in the intermediate hierarchical mesoporous beta zeolite; and'}treating the intermediate hierarchical mesoporous beta zeolite with an acidic solution to produce the hierarchical mesoporous beta zeolite comprising (e) a molar ratio of silicon to ...

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.

CATALYTIC MEMBRANE REACTOR FOR DIMETHYL ETHER SYNTHESIS FROM CARBON DIOXIDE AND HYDROGEN

Methods and systems or devices for synthesis of dimethyl ether (DME) from carbon dioxide and hydrogen are provided. A high surface area hollow fiber catalytic membrane reactor such as with hollow fibers coated with a water permeable membrane material is used. The reactor also contains a bi-functional methanol synthesis component and dehydration catalyst component such that the two-step reaction takes place on the catalyst surface. Produced water permeates through the membrane, exiting the reactor immediately after it is formed. Unreacted reactants and products flow to the reactor exit. 1. A system for synthesis of dimethyl ether from carbon dioxide and hydrogen , the system comprising:a catalytic membrane reactor including a plurality of channels and having an outer surface with a water permeable membrane coating, the reactor further containing a bi-functional catalyst material including a methanol synthesis catalyst component to catalyze reaction of carbon dioxide and hydrogen to form methanol and water and a dehydration catalyst component to catalyze dehydration of methanol to form dimethyl ether,wherein upon formation formed water permeates through the water permeable membrane coating and exits the reactor.2. The system of wherein the catalytic membrane reactor comprises at least one of: a) at least one reactor body including at least two of said channels and b) a plurality of hollow fibers claim 1 , each fiber forming at least one of said channels.3. The system of wherein the catalytic membrane reactor comprises at least one reactor body including at least two of said channels.4. The system of wherein each of the channels includes an inner surface claim 3 , wherein the bi-functional catalyst material is disposed on the inner surface of the channels claim 3 , and wherein formed water permeates through the reactor body and the water permeable membrane coating to a shell side of the reactor.5. The system of wherein the catalytic membrane reactor comprises a ...

Mesoporous Zeolite-Containing Catalysts For The Thermoconversion Of Biomass And For Upgrading Bio-Oils

Processes for making a catalytic system and catalytic systems for converting solid biomass into fuel of specialty chemical products are described. The catalyst system may comprise a non-zeolitic matrix and an in situ grown zeolite, such as MFI-type zeolite, with a meso-micro hierarchical pore structure. In some embodiments, the non-zeolitic matrix has a meso-macro hierarchical pore structure. 151-. (canceled)52. A composition for the conversion of biomass comprising:a. a catalyst system comprising a zeolite having a high silica to aluminum ratio and a hierarchical pore structure with pores having a size ranging from about 5 to 20 angstrom, a non-zeolitic matrix with a macroporosity from about 100 to about 5,000 angstrom pore size range, and a binder; and{'sup': '14', 'b. a feedstock having a carbon C isotope content of about 107 pMC.'}53. The composition of wherein the zeolite is MFI claim 52 , beta zeolite or mixtures thereof.54. The composition of wherein the matrix comprises silica claim 52 , alumina claim 52 , silica-alumina claim 52 , transitional metal oxide or a combination thereof.55. The composition of wherein the feedstock is a particulated biomass claim 52 , or is a product derived from pyrolysis of biomass.56. The composition of wherein the feedstock is a bio-oil vapor or a bio-oil.57. A process for upgrading bio-oil vapors claim 52 , the process comprising heating the bio-oil vapors in presence of the catalyst system claim 52 , the catalyst system comprising a zeolite having a hierarchical pore structure ranging from 5 to 20 angstrom pore size claim 52 , a non-zeolitic matrix with a hierarchical pore structure ranging from about 100 to about 5 claim 52 ,000 angstrom pore size claim 52 , and a binder.58128-. (canceled)129. A catalyst system comprising in situ crystallized zeolite having a hierarchical pore structure ranging from 20 to 1 claim 52 ,000 Angstrom pore size claim 52 , a non-zeolitic matrix having a hierarchical pore structure ranging from 50 ...

Process for producing ethylbenzene

A process for producing ethylbenzene is described in which benzene and ethylene are supplied to an alkylation reaction zone. Also added to the alkylation reaction zone is a C 3+ olefin in an amount of at least 200 ppm by weight of the ethylene supplied to the alkylation reaction zone. The benzene, ethylene and C 3+ olefin are contacted with an alkylation catalyst in the alkylation reaction zone to alkylate at least part of the benzene and produce an alkylation effluent comprising ethylbenzene, polyethylated benzene and at least one mono-C 3+ alkyl benzene. The alkylation effluent is separated into a first product fraction comprising ethylbenzene and a second fraction comprising polyethylated benzene and the at least one mono-C 3+ alkyl benzene. The second fraction is then contacted with benzene in the presence of a transalkylation catalyst to convert at least part of the polyethylated benzene to ethylbenzene and produce a transalkylation effluent.

A PROCESS FOR PREPARING A ZEOLITIC MATERIAL HAVING FRAMEWORK TYPE AEI

A process for preparing a zeolitic material having framework type AEI and having a framework structure which comprises a tetravalent element Y, a trivalent element X, and oxygen, said process comprising (i) providing a zeolitic material having framework type CHA and having a framework structure comprising the tetravalent element Y, the trivalent element X, and oxygen; (ii) preparing a synthesis mixture comprising the zeolitic material provided in (i), water, a source of the tetravalent element Y other than the zeolitic material provided in (i), and an AEI framework structure directing agent; (iii) subjecting the synthesis mixture prepared in (ii) to hydrothermal synthesis conditions comprising heating the synthesis mixture to a temperature in the range of from 100 to 200° C. and keeping the synthesis mixture at a temperature in this range under autogenous pressure, obtaining the zeolitic material having framework type AEI; wherein Y is one or more of Si, Ge, Sn, Ti, Zr; wherein X is one or more of Al, B, Ga, In; wherein in the framework structure of the zeolitic material provided in (i), the molar ratio Y:X, calculated as YO:XO, is at most 20:1. 1. A process for preparing a zeolitic material having framework type AEI and having a framework structure which comprises a tetravalent element Y , a trivalent element X. and oxygen , said process comprising(i) providing a zeolitic material having framework type CHA and having a framework structure comprising the tetravalent element Y, the trivalent element X, and oxygen;(ii) preparing a synthesis mixture comprising the zeolitic material provided in (i), water, a source of the tetravalent element Y other than the zeolitic material provided in (i), and an AEI framework structure directing agent;(iii) subjecting the synthesis mixture prepared in (ii) to hydrothermal synthesis conditions comprising heating the synthesis mixture to a temperature in the range of from 100 to 200° C. and keeping the synthesis mixture at a ...

SCR METHOD FOR REDUCING OXIDES OF NITROGEN AND METHOD FOR PRODUCING A CATALYST FOR SUCH METHOD

A method of reducing nitrogen oxides in exhaust gas of an internal combustion engine by selective catalytic reduction (SCR) comprises contacting the exhaust gas also containing ammonia and oxygen with a catalytic converter comprising a catalyst () comprising at least one crystalline small-pore molecular sieve catalytically active component (Z) having a maximum ring opening of eight tetrahedral basic building blocks, which crystalline small-pore molecular sieve catalytically active component (Z) comprising mesopores. 1. A method of reducing nitrogen oxides in exhaust gas of an internal combustion engine by selective catalytic reduction (SCR) , which method comprising contacting the exhaust gas also containing ammonia and oxygen with a catalytic converter comprising a catalyst comprising at least one crystalline small-pore molecular sieve catalytically active component (ZM ,I) having a maximum ring opening of eight tetrahedral basic building blocks , which crystalline small-pore molecular sieve catalytically active component (ZM ,I) comprising mesopores.2. The method according to claim 1 , wherein the at least one crystalline small-pore catalytically active component is an aluminosilicate zeolite claim 1 , a silicoaluminophosphate molecular sieve or an aluminophosphate molecular sieve (ZM claim 1 ,I).3. The method according to claim 1 , wherein the molecular sieve comprises a promoter metal.4. The method according to claim 3 , wherein the crystalline molecular sieve is ion-exchanged with the promoter metal.5. The method according to claim 3 , wherein the promoter metal is iron or copper.6. The method according to claim 1 , wherein the crystalline molecular sieve is one or more of the framework structures CHA claim 1 , AEI claim 1 , ERI or AFX.7. The method according to claim 1 , comprising an inorganic binder component (B claim 1 ,BA).8. The method according to claim 7 , in which the inorganic binder component (B claim 7 ,BA) comprises porous particles having a ...

Molecular Sieve, COK-5, Its Synthesis and Use

A molecular sieve having the structure of COK-5 is produced using, as a structure directing agent, at least one diquaternary ammonium compound selected from the group consisting of 1,4-bis(N-propylpyrrolidinium)butane dications, 1,4-bis(N-butylpyrrolidinium)butane dications and 1,5-bis(N-propylpyrrolidinium)pentane dications. 1. A molecular sieve having the structure of COK-5 , comprising in its pores at least one diquaternary ammonium compound selected from the group consisting of 1 ,4-bis(N-propylpyrrolidinium)butane dications , 1 ,4-bis(N-butylpyrrolidinium)butane dications and 1 ,5-bis(N-propylpyrrolidinium)pentane dications.2. The molecular sieve of claim 1 , further comprising crystals having an external surface area as determined by the t-plot method for nitrogen physisorption of about 100 to about 300 m/g.3. The molecular sieve of claim 1 , further comprising crystals having a total surface area as determined by the t-plot method for nitrogen physisorption of about 350 to about 650 m/g.5. The molecular sieve material of claim 4 , the tetravalent element Y comprises silicon and the trivalent element X comprises boron or aluminum.6. A molecular sieve having the structure of COK-5 having an X-ray diffraction pattern with a first composite peak with a maximum at 25.0 (±0.30) degrees 2-theta (2θ) which has an intensity above background of Imaxand which intersects a second composite peak with a maximum at 23.0 (±0.20) degrees 2-theta (2θ) to form a local minimum which has an intensity above background of Imin claim 4 , such that the Imin/Imaxratio is >0.7.7. A molecular sieve having the structure of COK-5 claim 4 , comprising crystals having an external surface area as determined by the t-plot method for nitrogen physisorption of at least 100 m/g and having an X-ray diffraction pattern with a single diffuse composite feature in the 2-theta (2θ) range from 21.5 to 25.5 degrees.8. The molecular sieve of claim 7 , comprising crystals having a total surface area as ...

Process and Catalyst for Methane Conversion to Aromatics

A process and catalyst for use therein for the production of aromatics via the oxidative coupling of methane and methane co-aromatization with higher hydrocarbons in a single reaction stage. First, methane is partially converted to ethane and ethylene on an OCM catalyst component, and the OCM intermediate mixture containing methane, ethane and ethylene is subsequently converted into aromatics on an aromatization catalyst component. The reaction may be conducted at 550-850° C. and at about 50 psig. The claimed process and catalyst used therein achieves high methane conversion at lower temperatures (less than 800° C.), higher methane conversion into the aromatic products and significant reductions in production cost when compared to the traditional two (or more) step processes. 1. A process for producing aromatics , the process comprising:a. providing a feed comprising methane and an oxidant;b. contacting the feed with a catalyst comprising an oxidative coupling of methane (“OCM”) component and an aromatization component under conditions, including a temperature of about 600-800° C., effective to convert at least part of the methane in the feed to a product comprising at least 7 wt. % of aromatics, based on the weight of the product, wherein the OCM catalyst component and aromatization catalyst component are contained within a single reactor, wherein the OCM catalyst component comprises at least one alkaline/rare earth metal oxide, wherein the aromatization catalyst component comprises at least one molecular sieve and at least one dehydrogenation component; andc. separating at least part of the aromatics from the product.2. The process of claim 1 , wherein the OCM catalyst component and the aromatization catalyst component are physically mixed within the reactor.3. The process of claim 1 , wherein multiple layers of OCM catalyst component are alternated with multiple layers of aromatization catalyst component claim 1 , forming a stacked bed of catalyst within the ...

STABILIZED METAL-EXCHANGED SAPO MATERIAL

Described are catalyst materials and catalytic articles comprising a metal exchanged SAPO material comprising a plurality of substitutional sites consisting essentially of Si(4Al) sites and substantially free of Si(0Al) sites. The materials and catalytic articles are useful in methods and systems to catalyze the reduction of nitrogen oxides in the presence of a reductant. 116-. (canceled)17. A process for stabilizing a selective catalytic reduction catalyst material comprising a SAPO material and an exchanged metal , the process comprising:exposing the SAPO material to dry ammonia; andion exchanging the SAPO material with a metal salt to provide a stabilized SAPO material.18. The process of claim 17 , wherein the metal of the metal salt is selected from the group consisting of Cu claim 17 , Fe claim 17 , Co claim 17 , Ce and Ni.19. The process of claim 18 , wherein the metal comprises copper.20. The process of claim 19 , wherein the SAPO material comprises SAPO-34.21. The process of claim 17 , wherein the stabilized SAPO material comprises a plurality of substitutional sites consisting essentially of Si(4Al) sites and substantially free of Si(0Al) sites.22. The process according to claim 21 , wherein the plurality of substitutional sites includes less than 5% Si(0Al) sites.23. The process according to claim 21 , wherein the plurality of substitutional sites includes less than 1% Si(0Al) sites.24. The process according to claim 17 , wherein the SAPO material has a structure type selected from the group consisting of AEI claim 17 , AFT claim 17 , AFX claim 17 , CHA claim 17 , EAB claim 17 , ERI claim 17 , KFI claim 17 , LEV claim 17 , SAS claim 17 , SAT claim 17 , and SAV.25. The process according to claim 24 , wherein the SAPO material has the CHA structure type.26. The process according to claim 25 , wherein the SAPO material is selected from the group consisting of SAPO-34 claim 25 , SAPO-44 claim 25 , and SAPO-47.27. The process according to claim 17 , wherein the ...

CRYSTALLINE MOLECULAR SIEVES AND SYNTHESIS THEREOF

Crystalline molecular sieves and their synthesis using quaternary N-methyl-diisoalkylammonium cations as organic structure directing agents are disclosed. The structure directing agent has the following structure (1): 2. The method of claim 1 , wherein crystallization of the molecular sieve is conducted in the presence of an oxide of silicon; fluoride ions; water; and at least one structure directing agent selected from N claim 1 ,N-dimethyl-diisopropylammonium cations claim 1 , N-ethyl-N-methyl-diisopropylammonium cations claim 1 , N-hydroxymethyl-N-methyl-diisopropylammonium cations claim 1 , and N claim 1 ,N-dimethyl-di-sec-butylammonium cations.3. The method of claim 2 , wherein the molecular sieve has a *BEA framework type claim 2 , a NON framework type claim 2 , or a STF framework type.4. The method of claim 1 , wherein crystallization of the molecular sieve is conducted in the presence of oxides of silicon and germanium; fluoride ions; water; and at least one structure directing agent selected from N-ethyl-N-methyl-diisopropylammonium cations and N claim 1 ,N-dimethyl-di-sec-butylammonium cations.5. The method of claim 4 , wherein the molecular sieve has a BEC framework type.6. The method of claim 1 , wherein crystallization of the molecular sieve is conducted in the presence of oxides of silicon and boron; fluoride ions; water; and at least one structure directing agent selected from N claim 1 ,N-dimethyl-diisopropylammonium cations claim 1 , N-ethyl-N-methyl-diisopropylammonium cations and N claim 1 ,N-dimethyl-di-sec-butylammonium cations.7. The method of claim 6 , wherein the molecular sieve has a DDR framework type claim 6 , an EUO framework type claim 6 , or a framework type of SSZ-36.8. The method of claim 1 , wherein crystallization of the molecular sieve is conducted in the presence of oxides of silicon and aluminum; fluoride ions; water; and at least one structure directing agent selected from N claim 1 ,N-dimethyl-diisopropylammonium cations claim ...

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 ...

PROCESS FOR THE PREPARATION OF A DEALUMINATED ZEOLITIC MATERIAL HAVING THE BEA FRAMEWORK STRUCTURE

The present invention relates to a method for the preparation of a treated zeolitic material having a BEA framework structure comprising the steps of: (i) providing a zeolitic material having a BEA framework structure, wherein the BEA framework structure comprises YO2 and X2O3, wherein Y is a tetravalent element, and X is a trivalent element, and wherein the zeolitic material having a BEA framework structure is obtainable and/or obtained from an organotemplate-free synthetic process; (ii) calcining the zeolitic material provided in step (i) at a temperature of 650° C. or more; and (iii) treating the calcined zeolitic material obtained from step (ii) with an aqueous solution having a pH of 5 or less, as well as to zeolitic materials per se preferably obtainable according to the inventive method and to their use, and to a process for converting oxygenates to olefins employing the inventive zeolitic materials. 1. A method for the preparation of a treated zeolitic material having a BEA framework structure comprising the steps of:{'sub': 2', '2', '3, '(i) providing a zeolitic material having a BEA framework structure, wherein the BEA framework structure comprises YOand XO, wherein Y is a tetravalent element, and X is a trivalent element, and wherein the zeolitic material having a BEA framework structure is obtainable and/or obtained from an organotemplate-free synthetic process;'}(ii) calcining the zeolitic material provided in step (i) at a temperature of 650° C. or more; and(iii) treating the calcined zeolitic material obtained from step (ii) with an aqueous solution having a pH of 5 or less.2. The method of claim 1 , wherein in step (ii) the zeolitic material provided in step (i) is calcined at a temperature comprised in the range of from 680° C. to 1000° C.3. The method of claim 1 , wherein calcining in step (ii) is conducted in an atmosphere containing 10 wt.-% or less of water.4. The method of claim 1 , wherein Y is selected from the group consisting of Si claim 1 ...

METHOD FOR PRODUCING BETA ZEOLITE

Provided is a method for producing a beta zeolite, which is a seed crystal addition method that is capable of reducing the environmental load as much as possible. A method for producing a beta zeolite according to the present invention comprises a step wherein a reaction mixture that contains a silica source, an alumina source, an alkali source and water and a seed crystal that is composed of a beta zeolite are mixed with each other and heated. A beta zeolite which comprises particles having a particle size of 10 μm or less in an amount of 90% or more on a volume basis in the particle size distribution as determined by a laser diffraction/scattering particle size distribution measuring method, and which is synthesized without using an organic structure-directing agent is used as the seed crystal. 1. A method for producing a beta zeolite , comprising:mixing a reaction mixture comprising a silica source, an alumina source, an alkali source and water with a seed crystal comprising a beta zeolite and heating the mixture,wherein a beta zeolite synthesized without using an organic structure-directing agent and comprising particles having a particle size of 10 μm or less in an amount of 90% or more on a volume basis in the particle size distribution as determined by a laser diffraction/scattering particle size distribution measuring method is used as the seed crystal.2. The method for producing a beta zeolite according to claim 1 , wherein a beta zeolite synthesized using an organic structure defining agent and calcined is further used as the seed crystal.3. The method for producing a beta zeolite according to claim 2 , wherein claim 2 , in the seed crystal claim 2 , the content of the beta zeolite synthesized without using an organic structure defining agent is 10% by mass or more.4. The method for producing a beta zeolite according to claim 1 , wherein compositions of the reaction mixture represented by molar ratios are in ranges:{'sub': 2', '2', '3, 'SiO/AlO=8 to 40'}{' ...

Hydrocarbon Dehydrocyclization in the Presence of Carbon Dioxide

The invention relates to converting non-aromatic hydrocarbon in the presence of CO 2 to produce aromatic hydrocarbon. CO 2 methanation using molecular hydrogen produced during the aromatization increases aromatic hydrocarbon yield. The invention also relates to equipment and materials useful in such upgrading, to processes for carrying out such upgrading, and to the use of such processes for, e.g., natural gas upgrading.

ALKYLATION CATALYST

Catalyst compositions with improved alkylation activity and corresponding methods for making such catalyst compositions are provided. The catalyst(s) correspond to solid acid catalysts formed by exposing a catalyst precursor with a zeolitic framework structure to a molten metal salt that includes fluorine, such as a molten metal fluoride. The resulting fluorinated solid acid catalysts can have improved alkylation activity while having a reduced or minimized amount of structural change due to the exposure to the molten metal fluoride. This is in contrast to fluorinated solid acid catalysts that are exposed to higher severity forms of fluorination, such as exposure to ammonium fluoride or HF. SnFis an example of a suitable molten metal fluoride. 1. A catalyst composition comprising an MWW framework structure , 0.1 wt % to 2.5 wt % fluorine relative to a weight of the catalyst composition , and a weight ratio of Sn to F in the catalyst composition of 0.1 to 2.0.2. The catalyst composition of claim 1 , wherein the catalyst composition comprises a weight ratio of Sn to F in the MWW framework structure of 0.1 to 2.0.3. The catalyst composition of claim 1 , wherein the catalyst composition comprises MCM-49 claim 1 , MCM-22 claim 1 , MCM-56 claim 1 , or a combination thereof.4. The catalyst composition of claim 1 , wherein the MWW framework structure comprises a silicon to aluminum ratio of 2 to 100.5. The catalyst composition of claim 1 , wherein at least one of the MWW framework structure and the catalyst composition comprises 2.5 wt % or less Sn.6. The catalyst composition of claim 1 , wherein the MWW framework structure comprises 0.1 wt % to 2.5 wt % fluorine.7. The catalyst composition of claim 1 , wherein the catalyst composition further comprises a binder.8. A method for making an alkylation catalyst claim 1 , comprising:exposing a catalyst precursor comprising a zeolitic framework structure to a molten metal salt comprising fluoride anion at a temperature of 275° C. ...

Molecular Sieve Material, Its Synthesis and Use

A molecular sieve material, EMM-17, has in its as-calcined form an X-ray diffraction pattern including the following peaks in Table 11: 3. The molecular sieve material of claim 2 , wherein X includes one or more of B claim 2 , Al claim 2 , Fe claim 2 , and Ga and Y includes one or more of Si claim 2 , Ge claim 2 , Sn claim 2 , Ti claim 2 , and Zr.4. The molecular sieve material of claim 2 , wherein X is aluminum and Y is silicon.7. The molecular sieve material of claim 6 , wherein X is aluminum and Y is silicon.8. The molecular sieve material of claim 6 , wherein X includes one or more of B claim 6 , Al claim 6 , Fe claim 6 , and Ga and Y includes one or more of Si claim 6 , Ge claim 6 , Sn claim 6 , Ti claim 6 , and Zr.9. The molecular sieve material of claim 6 , wherein Q is selected from the group consisting of 1-methyl-4-(pyrrolidin-1-yl)pyridinium cations claim 6 , 1-ethyl-4-(pyrrolidin-1-yl)pyridinium cations claim 6 , 1-propyl-4-(pyrrolidin-1-yl)pyridinium cations claim 6 , 1-butyl-4-(pyrrolidin-1-yl)pyridinium cations and mixtures thereof.10. A process for producing the molecular sieve material of claim 6 , the process comprising the steps of: [{'br': None, 'sub': 2', '2', '3, 'YO/XOat least 30;'}, {'br': None, 'sub': 2', '2, 'HO/YO4 to 10;'}, {'br': None, 'sup': '−', 'sub': '2', 'OH/YO0.1 to 1;'}, {'br': None, 'sub': '2', 'F/YO0 to 1; and'}, {'br': None, 'sub': '2', 'Q/YO0.1 to 1;'}], '(a) preparing a synthesis mixture capable of forming said material, said mixture comprising water, a source of hydroxyl ions, a source of an oxide of a tetravalent element Y, a source of a trivalent element X, optionally a source of fluoride ions, and a directing agent Q selected from the group consisting of 1-methyl-4-(pyrrolidin-1-yl)pyridinium cations, 1-ethyl-4-(pyrrolidin-1-yl)pyridinium cations, 1-propyl-4-(pyrrolidin-1-yl)pyridinium cations, 1-butyl-4-(pyrrolidin-1-yl)pyridinium cations and mixtures thereof, and said synthesis mixture having a composition, in terms of ...

EXHAUST SYSTEM FOR A COMPRESSION IGNITION ENGINE COMPRISING A WATER ADSORBENT MATERIAL

An exhaust system for a compression ignition engine comprising: a water adsorbent material; and a catalyst composition for treating an exhaust gas pollutant produced by the compression ignition engine; wherein the water adsorbent material is: (i) arranged to contact exhaust gas from the compression ignition engine before the catalyst composition; and (ii) in thermal communication with the catalyst composition. 120-. (canceled)21. A diesel engine exhaust system comprising an oxidation catalyst , wherein the oxidation catalyst comprises:a water adsorbent material;a catalyst composition for treating an exhaust gas pollutant produced by the diesel engine, wherein the catalyst composition comprises a platinum group metal (PGM) and a support material, wherein the platinum group metal (PGM) comprises platinum; anda substrate;wherein the catalyst composition and the water adsorbent material is each disposed on the substrate, wherein a first washcoat layer comprising the water adsorbent material is disposed on a second washcoat layer comprising the catalyst composition such that the water adsorbent material is arranged to contact exhaust gas from the diesel engine before the catalyst composition.22. A diesel engine exhaust system according to claim 21 , wherein the water adsorbent material comprises a zeolite.23. A diesel engine exhaust system according to claim 22 , wherein the zeolite has a silica to alumina ratio (SAR) of 100:1 to 8:1.24. A diesel engine exhaust system according to claim 22 , wherein the zeolite has a pore size of from 3 Å to 15 Å.25. A diesel engine exhaust system according to claim 22 , wherein the zeolite is be selected from the group consisting of faujasite claim 22 , clinoptilolite claim 22 , mordenite claim 22 , silicalite claim 22 , ferrierite claim 22 , zeolite X claim 22 , zeolite Y claim 22 , ultrastable zeolite Y claim 22 , beta zeolite claim 22 , AEI zeolite claim 22 , ZSM-5 zeolite claim 22 , ZSM-12 zeolite claim 22 , ZSM-20 zeolite claim 22 ...

NANO-SIZED ZEOLITE CATALYST HAVING A HIGH SILICA TO ALUMINA RATIO

A catalyst includes a zeolite, wherein the zeolite has: a CHA framework; a particle size less than or equal to 100 nanometers; and a silica to alumina mole ratio in the range of about 50:1 to about 150:1. The catalyst can include a metal dopant. The catalyst can be used for purifying a product by flowing a reactant across the catalyst to form the product; and condensing or separating the product. The product can be an olefin or alkenes with an increased carbon chain. The catalyst can be used for selective catalytic reduction of nitrogen oxide or a gas to liquid reaction. A method of producing the catalyst can include selecting the concentration of a crystal growth inhibitor based on the ratio of the silica precursor and an alumina precursor such that the zeolite crystals have a mean particle size less than or equal to 100 nanometers. 1. A catalyst comprising: a CHA framework;', 'a particle size less than or equal to 100 nanometers; and', 'a silica to alumina mole ratio in the range of about 50:1 to about 150:1., 'a zeolite, wherein the zeolite has2. The catalyst according to claim 1 , wherein the zeolite has a particle size less than or equal to 50 nanometers.3. The catalyst according to claim 1 , wherein zeolite further comprises a metal dopant.4. The catalyst according to claim 3 , wherein the dopant is selected from copper (Cu) claim 3 , nickel (Ni) claim 3 , iron (Fe) claim 3 , zinc (Zn) claim 3 , manganese (Mn) claim 3 , and molybdenum (Mo).5. A method of producing a catalyst comprising:combining a silica precursor and an alumina precursor, wherein the ratio of the silica precursor to the alumina precursor is in the range of about 50:1 to about 150:1;adding a crystal growth inhibitor;adding a structure directing agent; andcrystallizing the zeolite, wherein the zeolite crystals have a CHA framework and a mean particle size less than or equal to 100 nanometers.6. The method according to claim 5 , wherein the crystal growth inhibitor is polyethyleneimine.7. The ...

DIESEL OXIDATION CATALYST CONTAINING MANGANESE

The present invention relates to a diesel oxidation catalyst, which comprises a carrier body having a length L extending between a first end face a and a second end face b and a catalytically active material zone A arranged on the carrier body, wherein the material zone A contains palladium and platinum on a manganese-containing carrier oxide, wherein the carrier oxide consists of a carrier oxide component A and a carrier oxide component B and the carrier oxide component B consists of manganese and/or a manganese compound and is present in an amount of 5 to 15 wt. %, calculated as MnOand based on the total weight of the manganese-containing carrier oxide. 1. A diesel oxidation catalyst , which comprises a carrier body having a length L extending between a first end face a and a second end face b and a catalytically active material zone A arranged on the carrier body , wherein the material zone A contains palladium and platinum supported on a manganese-containing carrier oxide , wherein the manganese-containing carrier oxide consists of carrier oxide component A and a carrier oxide component B and the carrier oxide component B consists of manganese and/or a manganese compound and is present in an amount of 5 to 15 wt. % , calculated as MnOand based on the total weight of the manganese-containing carrier oxide.2. Diesel oxidation catalyst according to claim 1 , wherein the carrier oxide component A is selected from the series consisting of aluminum oxide claim 1 , doped aluminum oxide claim 1 , silicon oxide claim 1 , titanium dioxide and mixed oxides containing one or more of said oxides.3. Diesel oxidation catalyst according to claim 1 , wherein the carrier oxide component A is doped aluminum oxide.4. Diesel oxidation catalyst according to claim 1 , wherein the carrier oxide component A is a mixed oxide comprising aluminum oxide and silicon oxide or a silicon-oxide-doped aluminum oxide.5. Diesel oxidation catalyst according to claim 1 , wherein claim 1 , the carrier ...

METHODS TO PRODUCE MOLECULAR SIEVES WITH LTA TOPOLOGY AND COMPOSITIONS DERIVED THEREFROM

The present disclosure is directed to processing for preparing crystalline pure-silica and heteroatom-substituted LTA frameworks in fluoride media using a simple organic structure-directing agent (OSDA), having a structure of Formula (I): 1. A crystalline microporous silicate of LTA topology that is substantially free of an Organic Structure Directing Agent (OSDA).2. The crystalline microporous silicate of claim 1 , that is an aluminosilicate having a molar ratio of Si:Al in a range of from about 5 to about 50.3. The crystalline microporous aluminosilicate of claim 2 , having a molar ratio of Si:Al in a range of from about 12 to about 42.4. The crystalline microporous aluminosilicate of claim 2 , comprising pores containing Li claim 2 , Na claim 2 , K claim 2 , Rb claim 2 , Cs claim 2 , Be claim 2 , Mg claim 2 , Ca claim 2 , Sr claim 2 , Be claim 2 , Al claim 2 , Ga claim 2 , In claim 2 , Zn claim 2 , Ag claim 2 , Cd claim 2 , Ru claim 2 , Rh claim 2 , Pd claim 2 , Pt claim 2 , Au claim 2 , Hg claim 2 , La claim 2 , Ce claim 2 , Pr claim 2 , Nd claim 2 , Pm claim 2 , Sm claim 2 , Eu claim 2 , or RNHcations claim 2 , where R is alkyl claim 2 , and n=0-4.5. The crystalline microporous aluminosilicate of claim 2 , comprising pores containing NaCl or KCl.6. The crystalline microporous aluminosilicate of claim 2 , comprising pores containing scandium claim 2 , yttrium claim 2 , titanium claim 2 , zirconium claim 2 , vanadium claim 2 , manganese claim 2 , chromium claim 2 , molybdenum claim 2 , tungsten claim 2 , iron claim 2 , ruthenium claim 2 , osmium claim 2 , cobalt claim 2 , rhodium claim 2 , iridium claim 2 , nickel claim 2 , palladium claim 2 , platinum claim 2 , copper claim 2 , silver claim 2 , gold claim 2 , or a mixture thereof claim 2 , each as a metal claim 2 , oxide claim 2 , or salt.7. The crystalline microporous aluminosilicate of claim 2 , comprising pores containing copper as a metal claim 2 , oxide claim 2 , or salt.8. The crystalline microporous ...

PROCESS FOR PREPARATION OF ZEOLITIC MATERIAL

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

A METHOD FOR PRODUCING ZEOLITE CRYSTALS AND/OR ZEOLITE-LIKE CRYSTALS

The present invention pertains to a method for producing zeolite or zeolite-like crystals using a composition comprising one or more fluorine-containing compounds as a mineralizing agent. Crystals produced by such a method are smaller in size than crystals available in the art and contain few defects. The invention also relates to zeolite and/or zeolite-like crystals obtainable by a method as provided herein as well as crystals defined by any of the structural characteristics provided herein, and the usage thereof such as in the manufacture of thin films and membranes, absorbents, catalysts etc. 122.-. (canceled)23. A method for producing MFI zeolite crystals , wherein said method comprises the following steps: i) one or more tetraalkoxysilane(s) and/or one or more aluminiumalkoxide(s),', 'ii) tetraalkylammoniumhydroxide, and', 'iii) water,', 'thereby providing a mixture comprising', 'i) one or more hydrolyzed tetraalkoxysilane(s) and/or one or more hydrolysed aluminiumalkoxide(s),', 'ii) tetraalkylammoniumhydroxide,', 'iii) water, and', 'iv) one or more alcohol(s),, 'a) mixing'}b) removing said alcohol(s) formed in step a) so that the mixture contains 10 wt % or less of said alcohol(s), '(ii) adjusting the pH of the composition to which the fluorine containing compound has been added to a pH of 6-8,', 'd) (i) adding a fluorine containing compound to the mixture, said fluorine containing compound being selected from the group consisting of tetraalkylammonium fluoride, ammonium fluoride, potassium fluoride, sodium fluoride, and hydrofluoric acid, or a combination thereof, and'}e) forming MFI zeolite crystals from the mixture using hydrothermal treatment in a temperature range from 30° C. to 100° C., andf) collecting the MFI zeolite crystals from step e), wherein the MFI zeolite crystals have a length of 1.5 μm or less.24. The method according to claim 23 , further comprising a step c) prior to step d) and following step b):c) adding one or more aqueous solvent(s) to ...

Exhaust After-treatment System Having Low Temperature SCR Catalyst

An aftertreatment system for treating exhaust gas discharged from a combustion engine, the aftertreatment system comprising a low temperature selective-catalytic-reduction catalyst, wherein the low-temperature selective-catalytic-reduction catalyst is a mixture of catalytic metals provided on a beta-zeolite support material, the mixture of catalytic metals being at least one mixture selected from Cu and Ce, Mn and Ce, Mn and Fe, Cu and W, Mn and W, and Ce and W. 1. An aftertreatment system for treating exhaust gas discharged from a combustion engine , the aftertreatment system comprising a low temperature selective-catalytic-reduction catalyst , wherein the low-temperature selective-catalytic-reduction catalyst is a mixture of catalytic metals provided on a beta-zeolite support material , the mixture of catalytic metals being at least one mixture selected from Cu and Ce , Mn and Ce , Mn and Fe , Cu and W , Mn and W , and Ce and W.2. The aftertreatment system according to claim 1 , wherein a loading of each metal in each mixture is in the range of 0.5 to 20 wt % claim 1 , with the balance comprising the beta-zeolite support material.3. The aftertreatment system according to claim 1 , wherein a mass ratio of an amount of a first catalytic metal relative to an amount of a second catalytic metal in each mixture is in the range of 1.5 to 40.4. The aftertreatment system according to claim 1 , wherein a mass ratio of an amount of a first catalytic metal relative to an amount of a second catalytic metal in each mixture is in the range of 3 to 25.5. The aftertreatment system according to claim 1 , wherein a mass ratio of an amount of a first catalytic metal relative to an amount of a second catalytic metal in each mixture is in the range of 5 to 20.6. The aftertreatment system according to claim 1 , wherein the mixtures of catalytic metal are formed by at least one method selected from the group consisting of cation exchange claim 1 , deposition precipitation claim 1 , ...

CATALYTIC COMPOSITION AND STRUCTURES MADE THEREOF

Methods use a catalytic composition built up from a ceramic material including a catalytic material and a first inorganic binder and a second inorganic binder and a catalytic structure made thereof. Preferably, the structure is made by a colloidal ceramic shaping technique. The structure is used for catalytic or ion exchange applications. The catalytic structures have excellent mechanical, physicochemical and catalytic properties. 1. A method for performing methanol-to-olefins reactions , comprising:{'claim-text': ['shaping a composition comprising a ceramic material to obtain a green structure, wherein said ceramic material comprises a catalytic material and a first inorganic binder and a second inorganic binder, the shaping comprising preparing a suspension, slurry or paste of the composition and extruding the suspension, slurry or paste as fibers by three-dimensional fiber deposition to obtain the green structure, wherein the fibers are spaced apart to form a porous layered network;', 'the total amount of the first and second inorganic binders in the ceramic material comprising between 10 wt % and 50 wt % by total solid weight of the formed catalytic structure;', 'wherein the first inorganic binder is a clay material and the second inorganic binder is selected from: colloidal silica, colloidal alumina, colloidal zirconia, colloidal yttrium oxide, or colloidal tin oxide; or the first inorganic binder is selected from: colloidal silica, colloidal alumina, colloidal zirconia, colloidal yttrium oxide and the second inorganic binder is an inorganic thermohardening compound;', 'drying and calcining the green structure to obtain the bulk catalytic structure, wherein the structure is monolithic and comprises first channels having a length extending in a flow direction and second channels having a length extending in a radial direction, wherein the first channels and the second channels are fluidly connected; and'], '#text': 'building a bulk catalytic structure, ...

MOLECULAR SIEVE SSZ-120, ITS SYNTHESIS AND USE

A small crystal size, high surface area aluminogermanosilicate molecular sieve material, designated SSZ-120, is provided. SSZ-120 can be synthesized using 3,3′-[2,6-naphthalenebis(methylene)]bis[1,2-dimethyl-1H-imidazolium] dications as a structure directing agent. SSZ-120 may be used in organic compound conversion reactions and/or sorptive processes. 2. The organic nitrogen compound of claim 1 , wherein the dication is associated with anionic counterion selected from hydroxide claim 1 , chloride claim 1 , bromide claim 1 , or a combination thereof. This application is a divisional application of U.S. patent application Ser. No. 17/323,005 filed on May 18, 2021, which claims priority to and the benefit of U.S. Provisional Application Ser. No. 63/028,642 filed on May 22, 2020.This disclosure relates to a small crystal size, high surface area aluminogermanosilicate molecular sieve designated SSZ-120, its synthesis, and its use in organic compound conversion reactions and sorption processes.Molecular sieves are a commercially important class of materials that have distinct crystal structures with defined pore structures that are shown by distinct X-ray diffraction (XRD) patterns and have specific chemical compositions. The crystal structure defines cavities and pores that are characteristic of the specific type of molecular sieve.According to the present disclosure, a small crystal size, high surface area aluminogermanosilicate molecular sieve, designated SSZ-120 and having a unique powder X-ray diffraction pattern, has been synthesized using 3,3′-[2,6-naphthalenebis(methylene)]bis[1,2-dimethyl-1H-imidazolium] dications as a structure directing agent.In a first aspect, there is provided an aluminogermanosilicate molecular sieve having, in its calcined form, a powder X-ray diffraction pattern including the peaks in the following table:The calcined molecular sieve can have a total surface area (as determined by the t-plot method for nitrogen physisorption) of at least ...

METHODS, SYSTEMS, AND CATALYSTS FOR THE DIRECT CONVERSION OF SYNGAS TO HIGH-OCTANE HYDROCARBONS

The present disclosure relates to a method that includes converting a gas stream that contains hydrogen (H) and carbon monoxide (CO) to a second mixture that contains a hydrocarbon, for example, a hydrocarbon having between 3 and 15 carbon atoms, where the converting is performed using a first catalyst configured to convert Hand CO to methanol, a second catalyst configured to convert methanol to dimethyl ether (DME), and a third catalyst configured to convert DME to the hydrocarbon. 1. A method comprising:{'sub': '2', 'converting a gas stream comprising hydrogen (H) and carbon monoxide (CO) to a second mixture comprising a hydrocarbon having between 3 and 15 carbon atoms, wherein{'sub': '2', 'the converting is performed using a first catalyst configured to convert Hand CO to methanol,'}a second catalyst configured to convert methanol to dimethyl ether (DME), anda third catalyst configured to convert DME to the hydrocarbon.2. The method of claim 1 , wherein the first catalyst comprises copper and a zinc oxide.3. The method of claim 2 , wherein the first catalyst further comprises at least one of silica claim 2 , alumina claim 2 , zirconia claim 2 , or ceria.4. The method of claim 1 , wherein the second catalyst comprises at least one of an alumina or silica.5. The method of claim 1 , wherein the third catalyst comprises at least one of copper or a zeolite.6. The method of claim 5 , wherein the zeolite comprises a beta zeolite having a silica to alumina ratio between about 20:1 and about 300:1.7. The method of claim 6 , wherein the copper in the third catalyst is present at a concentration between about 1 wt % and about 20 wt % claim 6 , relative to the total weight of the third catalyst.8. The method of claim 1 , wherein the first catalyst and the second catalyst are present at a ratio between about 1:1 and about 8:1.9. The method of claim 8 , wherein the second catalyst and the third catalyst are present at a ratio between about 0.1:1 and about 5:2.10. The method of ...

EMM-23 MATERIALS AND PROCESSES AND USES THEREOF

The disclosure is related to various modified EMM-23 materials, processes, and uses of the same. 1. A process of preparing a modified EMM-23 material comprising a composition of Formula II:{'br': None, 'sub': 2', '3', '2, 'XO:(m)YO\u2003\u2003(Formula II),'} {'br': None, 'sub': 2', '3', '2, 'XO:(t)YO\u2003\u2003(Formula III),'}, 'comprising combining a composition of Formula (III)with an agent comprising X to generate a material of Formula II;wherein m is less than 150, t is greater than or equal to 150, X is a trivalent element, and Y is a tetravalent element.2. The process of further comprises adjusting the pH of the combination of the composition of Formula III and the agent comprising X to within the range of 2.4 to 2.6.3. The process of claim 1 , wherein the agent comprises Al(NO) claim 1 , Al(SO) claim 1 , AlCl claim 1 , Fe(NO) claim 1 , or a mixture thereof.4. The process of further comprises combining additional amount of the agent comprising X to the pH adjusted combination of the composition of Formula III claim 1 , and adjusting the pH of the combination having additional amount of the agent comprising X to within the range of 2.4 to 2.6.5. The process of claim 4 , wherein the process of combining additional amount of the agent comprising X and adjusting the pH of the combination to within the range of 2.4 to 2.6 is repeated until the pH does not change when additional amount of the agent comprising X is added.6. The process of claim 4 , wherein the adjusting of the pH comprises adding a base or an acid to the combination of the composition of Formula III and the agent comprising X.7. The process of claim 6 , wherein the adjusting of the pH comprises adding a base.8. The process of claim 7 , wherein the base comprises an organic amine base.9. The process of claim 7 , wherein the base comprises ammonium hydroxide.10. The process of further comprises heating the pH adjusted combination of the composition of Formula III and the agent comprising X at a ...