КАТАЛИЗАТОР ГИДРООЧИСТКИ, СОДЕРЖАЩИЙ ПОДЛОЖКУ, ПОЛУЧЕННУЮ ИЗ АЛЮМОГЕЛЯ, И СПОСОБ ПОЛУЧЕНИЯ ТАКОГО КАТАЛИЗАТОРА

Настоящее изобретение относится к катализатору гидродесульфирования, содержащему подложку, фосфор, по меньшей мере, один металл, выбранный из группы VIB, причем металлом группы VIB является молибден, и, по меньшей мере, один металл, выбранный из группы VIII периодической системы элементов, причем металлом группы VIII является кобальт, причем содержание металла группы VIB, выраженного в расчете на содержание оксидов, составляет от 6 до 25 вес.% от общего веса катализатора, содержание металла группы VIII, выраженное в расчете на содержание оксидов, составляет от 0,5 до 7 вес.% от общего веса катализатора, подложка содержит по меньшей мере 90 вес.% оксида алюминия, который получен из размешанного и экструдированного геля бемита, и причем плотность молибдена в катализаторе, выраженная в числе атомов молибдена на нмкатализатора, составляет от 3 до 5, атомное соотношение Co/Mo составляет от 0,3 до 0,5, и атомное соотношение P/Mo составляет от 0,1 до 0,3, и удельная поверхность указанного катализатора ...

МЕЗОПОРИСТЫЙ КАТАЛИЗАТОР НА ОСНОВЕ СМЕШАННОГО ОКСИДА, СОДЕРЖАЩИЙ КРЕМНИЙ

Изобретение относится к мезопористым катализаторам для получения бутадиена из этанола. Предложен мезопористый катализатор на основе смешанного оксида, содержащего кремний и по меньшей мере один металл M, выбранный из тантала, ниобия и их смесей, в котором массовое содержание металла M составляет от 0,1 и 20% от массы смешанного оксида, и кремний и металл М связаны ковалентной связью. Предложен также способ получения указанного катализатора и его применение для получения 1,3-бутадиена из этанола. Технический результат – снижение стоимости катализатора при сохранении его эффективности. 3 н. и 10 з.п. ф-лы, 4 табл., 9 пр., 1 ил.

СТАБИЛИЗИРОВАННОЕ ПОЛУЧЕНИЕ 1,3-БУТАДИЕНА В ПРИСУТСТВИИ ОКСИДА ТАНТАЛА, ЛЕГИРОВАННОГО АЛЬДОЛИЗИРУЮЩИМ ЭЛЕМЕНТОМ

Изобретение относится к катализатору для превращения сырья, содержащего по меньшей мере этанол, в бутадиен и к его применению. Катализатор содержит по меньшей мере элемент тантал, по меньшей мере один альдолизирующий элемент, выбранный из группы, состоящей из кальция, бария и их смесей, и по меньшей мере одну мезопористую оксидную матрицу, содержащую по меньшей мере один оксид элемента X, выбранного из кремния, титана и их смесей. Массовое содержание элемента тантал составляет от 0,3% до 10% от массы мезопористой оксидной матрицы, а массовое содержание альдолизирующего элемента составляет от 0,05% до 4% от массы мезопористой оксидной матрицы. Изобретение относится также к применению указанного катализатора для превращения этанола в 1,3-бутадиен при температуре от 300°C до 400°C, давлении от 0,15 до 0,5 МПа, объемной скорости от 0,5 до 5 ч. Технический результат - повышение продолжительности цикла (поддержание селективности на экономически приемлемом уровне в течение более длительного времени ...

КАТАЛИЗАТОР НА ОСНОВЕ МЕДИ, НАНЕСЕННЫЙ НА МЕЗОПОРИСТЫЙ УГОЛЬ, СПОСОБ ЕГО ПОЛУЧЕНИЯ И ПРИМЕНЕНИЯ

Данное изобретение относится к нанесенному на мезопористый уголь катализатору на основе меди, к способу его получения и применению в каталитическом дегидрировании соединения с алкильной цепью C-Cдля превращения соединения с алкильной цепью C-Cв соединение с соответствующей алкенильной цепью. Катализатор включает мезопористый уголь, медный компонент и вспомогательный элемент, нанесенные на указанный мезопористый уголь. Один или несколько вспомогательных элементов (в виде оксидов) выбирают из группы, состоящей из VO, LiO, MgO, СаО, GaO, ZnO, AlО, CeO, LaO, SnOи KO. Количество медного компонента (в расчете на CuO) составляет 2-20 мас.% в расчете на общую массу катализатора. Количество вспомогательного элемента (в расчете на указанный оксид) составляет 0-3 мас.%. Количество мезопористого угля составляет 77.1-98 мас.% в расчете на общую массу катализатора. Способ получения катализатора включает: (1) стадию контактирования предшественника медного компонента, предшественника вспомогательного элемента ...

ЧАСТИЦЫ ОКСИДА ЦЕРИЯ И СПОСОБ ИХ ПОЛУЧЕНИЯ

Настоящее изобретение относится к частицам оксида церия, которые имеют превосходную термостойкость, в частности, пригодным для катализаторов, функциональной керамики, твердого электролита для топливных элементов, материала для шлифовки, поглотителей ультрафиолетового излучения, и тому подобное, и особенно пригодным для использования в качестве материала катализатора или сокатализатора, например, при катализе для очистки выхлопных газов транспортных средств. Настоящее изобретение также относится к способу получения таких частиц оксида церия, и к катализатору, например, для очистки выхлопных газов, с использованием таких частиц оксида церия. Способ получения частиц оксида церия включает по меньшей мере стадии подготовки раствора соли церия, содержащей анионы и катионы, где в пределах от 90 до 100% мольн. катионов церия представляют собой четырехвалентные катионы церия. Способ также включает нагревание раствора соли церия при температуре, заключенной в пределах от 60 до 220°C, с получением ...

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРОВ КАТАЛИТИЧЕСКОГО КРЕКИНГА СО ВЗВЕШЕННЫМ СЛОЕМ С УМЕНЬШЕННЫМИ СКОРОСТЯМИ ИЗНАШИВАНИЯ

Каталитическая микросфера каталитического крекинга со взвешенным катализатором, содержащая цеолит, где указанная микросфера сформирована из пульпы, содержащей: i) каолин, который прокаливали вне его экзотермического перехода; и или ii) кристаллы цеолита, или iii) гидратированный каолин и/или метакаолин, пульпа была смешана с 0.005-0.5 мас.% катионоактивного полиэлектролита относительно массы i) + ii) или i) + iii) перед или во время формирования указанной микросферы. Также представлен способ получения каталитической микросферы. Технический результат - обеспечить катализаторы каталитического крекинга со взвешенным слоем, имеющим улучшенную устойчивость к изнашиванию. 2 н. и 16 з.п. ф-лы, 8 табл., 4 ил., 2 пр.

КАТАЛИЗАТОРЫ, КОТОРЫЕ СОДЕРЖАТ ГАЛОГЕНИДСОДЕРЖАЩИЕ ВОЛЬФРАМАТЫ ЩЕЛОЧНЫХ МЕТАЛЛОВ, ДЛЯ СИНТЕЗА АЛКИЛМЕРКАПТАНОВ И СПОСОБ ИХ ПРИГОТОВЛЕНИЯ

Изобретение относится к катализатору, содержащему вольфрамат щелочного металла, содержащему по меньшей мере один галогенид, где щелочнометаллический компонент выбран из группы, включающей Cs, Rb, или под щелочнометаллическим компонентом подразумевается комбинация из двух связанных щелочных металлов, в том числе и в отличном от 1:1 соотношении между ними, выбранная из группы, включающей а) калий и цезий, б) натрий и цезий, в) рубидий и цезий. Также изобретение раскрывает способ приготовления содержащего вольфрамат щелочного металла нанесенного катализатора и способ получения алкилмеркаптанов. Катализатор обладает высокой активностью и селективностью, что позволяет повысить выход алкилмеркаптанов и экономическую эффективность процесса их получения. 3 н. и 25 з.п. формулы, 1 табл.

СПОСОБ ПОЛУЧЕНИЯ ОЛЕФИНОКСИДА, СПОСОБ ПРИМЕНЕНИЯ ОЛЕФИНОКСИДА И КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ

Изобретение относится к способам получения каталитической композиции, к способу получения олефиноксида и к способу получения 1,2-диола или простого эфира 1,2-диола. Описан способ получения каталитической композиции, включающий осаждение серебра на носитель и осаждение промотора - щелочного металла на носитель, причем щелочной металл содержит калий в количестве, по меньшей мере, 10 мкмоль/г и литий в количестве, по меньшей мере, 1 мкмоль/г в расчете на массу каталитической композиции, при этом щелочной металл осаждают на носитель до осаждения серебра, одновременно с осаждением серебра или после осаждения серебра на носитель. Описан способ получения каталитической композиции, предусматривающий использование в качестве промотора калия в количестве, по меньшей мере, 10 мкмоль/г и натрия в количестве, по меньшей мере, 5 мкмоль/г в расчете на массу каталитической композиции. Описан способ получения олефиноксида взаимодействием олефина, имеющего не менее трех углеродных атомов, с кислородом в ...

КОМПЛЕКСНЫЙ СПОСОБ КРЕКИНГА С ПСЕВДООЖИЖЕННЫМ КАТАЛИЗАТОРОМ ДЛЯ ПОЛУЧЕНИЯ СМЕСЕЙ УГЛЕВОДОРОДОВ, ОБЛАДАЮЩИХ ВЫСОКИМ ТОПЛИВНЫМ КАЧЕСТВОМ

... 1. Комплексный способ превращения углеводородных фракций, происходящих из нефти, в смеси углеводородов, обладающие высоким топливным качеством, который включает следующие стадии: ! 1) проведение крекинга с псевдоожиженным катализатором (КПК) углеводородной фракции с получением смеси, содержащей ЛРГ (легкий рецикловый газойль); ! 2) разделения смеси, полученной на предшествующей стадии КПК, с целью выделения по меньшей мере одной фракции ЛРГ и фракции ТРГ (тяжелого рециклового газойля); ! 3) возможно, повторную подачу по меньшей мере части фракции ТРГ на стадию КПК; ! 4) проведение гидроочистки фракции ЛРГ; ! 5) проведение реакции продукта, полученного на стадии (4), с водородом, в присутствии каталитической системы, включающей: ! a) один или более металлов, выбранных из Pt, Pd, Ir, Ru, Rh и Re; ! b) алюмосиликат кислой природы, выбранный из цеолита, принадлежащего к семейству MTW, и полностью аморфного микро-мезопористого алюмосиликата, имеющего мольное соотношение SiO2/Al2O3 в диапазоне ...

СПОСОБ ПОЛУЧЕНИЯ АЛКЕНОВ ИЗ ОКСИГЕНАТОВ С ИСПОЛЬЗОВАНИЕМ НАНЕСЕННЫХ НА НОСИТЕЛЬ ГЕТЕРОПОЛИКИСЛОТНЫХ КАТАЛИЗАТОРОВ

... 1. Способ получения алкена (алкенов) из оксигенатного исходного материала в реакторе в присутствии нанесенного на носитель гетерополикислотного катализатора, отличающийся тем, что удельный объем его пор удовлетворяет следующей формуле: ! ОП>0,6-0,3 [количество ГПК/площадь поверхности высушенного катализатора], ! где ОП обозначает удельный объем пор высушенного, нанесенного на носитель гетерополикислотного катализатора (мл/г катализатора); ! количество ГПК представляет собой количество гетерополикислоты, содержащейся в высушенном, нанесенном на носитель гетерополикислотном катализаторе (мкмоль/г); ! площадь поверхности высушенного катализатора является удельной площадью поверхности высушенного, нанесенного на носитель гетерополикислотного катализатора (м2/г). ! 2. Способ по п.1, в котором количество гетерополикислоты на площадь поверхности нанесенного на носитель гетерополикислотного катализатора превышает 0,1 мкмоль/м2. ! 3. Способ по п.1, в котором нанесенный на носитель гетерополикислотный ...

КАТАЛИЗАТОР СИНТЕЗА ФИШЕРА-ТРОПША НА ОСНОВЕ КОБАЛЬТА, ПОКРЫТЫЙ МЕЗОПОРИСТЫМИ МАТЕРИАЛАМИ, И СПОСОБ ЕГО ПОЛУЧЕНИЯ

Описан катализатор синтеза Фишера-Тропша на основе кобальта, покрытый мезопористым материалом, и способ его получения. Катализатор содержит кремнеземный носитель, насыщенный на поверхности активным компонентом кобальта и селективным промотором циркония; снаружи активный компонент кобальта и селективный промотор циркония покрыт слоем оболочки мезопористого материала. Способ получения включает в себя получение кремнеземного носителя, насыщенного цирконием, получение первичного катализатора синтеза Фишера-Тропша на основе кобальта на кремнеземном носителе, приготовление раствора-прекурсора мезопористых материалов, дальнейшее погружение, кристаллизацию, промывку, сушку и прокаливание для получения катализатора синтеза Фишера-Тропша на основе кобальта с покрытием мезопористых материалов. Активный компонент покрыт и защищен слоем оболочки мезопористого материала, толщина слоя оболочки регулируется, катализатор имеет длительный срок службы, высокую реакционную способность и хорошую стабильность ...

УЛУЧШЕННЫЙ КАТАЛИЗАТОР ДЛЯ СЕЛЕКТИВНОГО ОКИСЛЕНИЯ СЕРОВОДОРОДА

Данное изобретение относится к области селективного окисления серосодержащих соединений, в частности сероводорода. Изобретение касается неподвижного слоя катализатора для селективного окисления сероводорода кислородом, причем данный составной слой катализатора содержит слой первого катализатора и слой второго катализатора, где слой первого катализатора включает частицы первого катализатора, которые содержат первый материал носителя, содержащий кремнезем, и первый оксид металла, содержащий FeO, и слой второго катализатора включает частицы второго катализатора, которые содержат второй материал носителя, содержащий кремнезем, и второй оксид металла, содержащий FeO, где указанные частицы первого катализатора имеют более высокую загрузку FeOв расчете на общую массу частиц первого катализатора, чем загрузка FeOдля указанных частиц второго катализатора в расчете на общую массу частиц второго катализатора, при этом указанная загрузка FeOдля частиц второго катализатора составляет менее чем 3% в ...

CПОСОБ ПРОИЗВОДСТВА НЕНАСЫЩЕННОГО УГЛЕВОДОРОДА И ОКСИГЕНИРОВАННОГО СОЕДИНЕНИЯ, КАТАЛИЗАТОР И СПОСОБ ЕГО ПРОИЗВОДСТВА

... 1. Способ производства ненасыщенного углеводорода и содержащего кислород соединения, отличающийся тем, что данный способ включает:первую стадию диспергирования катализатора в поли-α-олефине и восстановления катализатора моноксидом углерода или синтез-газом, причем катализатор получают путем нанесения железа на носитель, содержащий марганец и имеющий средний размер пор от 2 до 100 нм; ивторую стадию приведения катализатора после восстановления на первой стадии в контакт с синтез-газом в условиях температуры реакции от 100 до 600°С и давления при реакции от 0,1 до 10 МПа с получением продукта реакции, содержащего ненасыщенный углеводород и содержащее кислород соединение.2. Способ производства ненасыщенного углеводорода и содержащего кислород соединения по п.1, отличающийся тем, что температуру реакции на второй стадии поддерживают в интервале 280°С плюс или минус 20°С.3. Способ производства ненасыщенного углеводорода и содержащего кислород соединения по п.1 или 2, отличающийся тем, что катализатор ...

МЕЗОПОРИСТЫЙ И МАКРОПОРИСТЫЙ КАТАЛИЗАТОР С АКТИВНОЙ ФАЗОЙ, ПОЛУЧЕННЫЙ ПУТЕМ СОВМЕСТНОГО РАСТИРАНИЯ, СПОСОБ ЕГО ПРОИЗВОДСТВА И ЕГО ИСПОЛЬЗОВАНИЕ ДЛЯ ГИДРООЧИСТКИ ОСТАТКОВ

КАТАЛИЗАТОР И СПОСОБ ИЗОМЕРИЗАЦИИ

... 1. Катализатор изомеризации алкилароматических соединений, который содержит: ! по меньшей мере 50 мас.% кислого неорганического связующего; ! по меньшей мере 0,01 мас.% металла VIII группы; и ! 1-9 мас.% цеолита ZSM-12; ! причем цеолит ZSM-12 имеет молярное отношение окиси Si к окиси Al (SAR) от 60 до 200. ! 2. Катализатор по п.1, который представляет собой экструдат. ! 3. Катализатор по п.1 или 2, в котором пористость неорганического связующего составляет по меньшей мере 0,6 см3/г. ! 4. Катализатор по п.1 или 2, котором объемная плотность составляет менее 0,3 г/см3. ! 5. Катализатор по п.1 или 2, котором значение SAR составляет от 70 до 150. ! 6. Катализатор по п.1 или 2, который содержит 1-7 мас.% цеолита. ! 7. Катализатор по п.1 или 2, в котором цеолит ZSM-12 имеет средний размер кристаллов от 30 до 70 нм. ! 8. Катализатор по п.1 или 2, в котором кристалличность цеолита ZSM-12 составляет более 94%. ! 9. Способ изомеризации алкилароматических соединений для получения реакционной смеси ...

КАТАЛИЗАТОР НА ПОДЛОЖКЕ ИЗ ОКСИДА АЛЮМИНИЯ, ПОКРЫТОЙ ДИОКСИДОМ КРЕМНИЯ

... 1. Катализатор, включающий:(I) подложку катализатора, содержащую (а) ядро, которое включает частицы,оксида алюминия и (b) около 1-40 мас.% диоксида кремния относительно массы указанной подложки катализатора с покрытием на поверхности указанного ядра; площадь поверхности BET указанной покрытой подложки катализатора составляет более 20 м/г; пористость составляет, по меньшей мере, около 0,2 см/г; и величина нормированного поглощения серы (NSU) составляет до 25 мкг/м; и(II) 0,1-10 мас.% относительно массы указанного катализатора, каталитически активного элементарного переходного металла или его соединения, или его комплекса на поверхности указанной подложки катализатора с покрытием.2. Катализатор по п.1, в котором указанные частицы оксида алюминия включают частицы со средним размером частиц 1-500 мкм или агломератов частиц со средним размером частиц 1-10 мм или их смеси.3. Катализатор по п.1, в котором на указанные частицы оксида алюминия в виде первичных частиц вначале нанесено покрытие, и ...

ПОВЕРХНОСТНО-МОДИФИЦИРОВАННЫЙ КАРБОНАТ КАЛЬЦИЯ В КАЧЕСТВЕ НОСИТЕЛЯ ДЛЯ КАТАЛИЗАТОРОВ НА ОСНОВЕ ПЕРЕХОДНЫХ МЕТАЛЛОВ

ПОДЛОЖКА КАТАЛИЗАТОРА ИЗ ОКСИДА АЛЮМИНИЯ

... 1. Пористый оксид алюминия с высокой удельной поверхностью и с высоким объемом пор, содержащий:оксид алюминия,необязательно, оксид кремния и алюмосиликаты, инеобязательно, одну или более легирующих добавок,причем указанный оксид алюминия имеет удельную площадь поверхности от примерно 100 до примерно 500 м2/г и общий объем пор после обжига при 900°C в течение 2 часов равный или больший 1,2 см3/г, причем 15% или менее от общего объема пор составляют поры, имеющие диаметр менее 10 нанометров.2. Оксид алюминия по п.1, отличающийся тем, что указанный оксид алюминия имеет после обжига при 900°C в течение 2 часов общий объем пор, больший или равный 1,25 см3/г3. Оксид алюминия по п.1, отличающийся тем, что, после обжига при 900°C в течение 2 часов, 10% или менее от общего объема пор в указанном оксиде алюминия составляют поры, имеющие диаметр менее 10 нанометров.4. Оксид алюминия по п.1, отличающийся тем, что, после обжига при 900°C в течение 2 часов, 50% или менее от общего объема пор в указанном ...

ПОДЛОЖКА КАТАЛИЗАТОРА ИЗ ОКСИДА АЛЮМИНИЯ, УСТОЙЧИВАЯ К СЕРЕ

... 1. Способ получения устойчивого к сере оксида алюминия, включающий:получение гидрата алюминия из одной или более водорастворимых солей алюминия, причем каждая из указанных солей содержит катион алюминия или анион алюминия и противоположно заряженный противоион, в водной среде,приведение в контакт гидрата алюминия с предшественником оксида кремния в водной среде и в присутствии противоионов указанных одной или более солей алюминия,выделение частиц гидрата алюминия, вступившего в контакт с предшественником оксида кремния, из водной среды, иобжиг частиц гидрата алюминия, вступившего в контакт с предшественником оксида кремния, с получением частиц устойчивого к сере оксида алюминия.2. Способ по п.1, отличающийся тем, что указанный гидрат алюминия получают путем взаимодействия сульфата алюминия и алюмината натрия в водной среде.3. Способ по п.1, отличающийся тем, что указанный предшественник оксида кремния выбран из силикатов щелочных металлов и смесей указанных соединений.4. Способ по п.1, ...

СЕРОСОДЕРЖАЩАЯ КРЕМНЕЗЕМНАЯ ФРАКЦИЯ

... 1. Состав, содержащий вещество, имеющее эмпирическую формулу (SiO)(OH)MOF, где М присутствует в качестве необходимости и упомянутый М представляет собой катион, по меньшей мере, одного из следующих металлов или металлоидов: бор, магний, алюминий, кальций, титан, ванадий, марганец, железо, кобальт, никель, медь, цинк, цирконий, молибден, палладий, серебро, кадмий, олово, платина, золото и висмут, где F присутствует в случае необходимости и указанный F представляет собой, по меньшей мере, одно из следующих соединений: функционализованный органосилан, серосодержащий органосилан, аминосодержащий органосилан и алкилсодержащий органосилан с покрытием поверхности от 0,01% до 100%, и где молярное отношение y/x составляет от 0,01 до 0,5, молярное отношение x/z составляет от 0,1 до 300, а молярное отношение a/z зависит от свойства определенного оксида металла.2. Состав по п.1, в котором указанное вещество представляет собой водную суспензию с содержанием указанного вещества от 3% по массе до 15% ...

КАТАЛИЗАТОР ПРЕВРАЩЕНИЯ СИНТЕЗ-ГАЗА В СПИРТЫ

VERFAHREN ZUR HERSTELLUNG VON ALDEHYDEN.

Prepn. is claimed of aldehydes by gas-phase hydrogenation of aromatic carboxylic acids, or aliphatic carboxylic acids which possessup to one hydrogen atom alpha to the carboxyl or esters or anhydrides of these acids, at temps. of 300 to 450 deg.C and pressures of 0.1 10 bar aided by special iron as catalysts. Cpds are prepd. by burning carbonyls in air and oxygen to the required level of iron oxide, and may be impregnated into an inert carrier of suitable particle size and mixed with an appropriate lubricant for use in a fluidised bed reactor.

Katalysatorsystem

Katalysatorsystem, insbesondere geträgerter Katalysator, wobei das Katalysatorsystem mindestens eine auf einem Katalysatorträger aufgebrachte katalytisch aktive Komponente, insbesondere mindestens eine an einem Katalysatorträger fixierte katalytisch aktive Komponente, aufweist, wobei die katalytisch aktive Komponente mindestens ein Metall umfasst und/oder hieraus besteht, wobei das Katalysatorsystem erhältlich ist durch ein Verfahren, wobei zunächst eine als Katalysatorträger eingesetzte kugelförmige Aktivkohle einer Oxidation, insbesondere Oberflächenoxidation, unterzogen wird und wobei nachfolgend die auf diese Weise erhaltene oxidierte, insbesondere an ihrer Oberfläche oxidierte Aktivkohle mit der katalytisch aktiven Komponente ausgerüstet und/oder beladen und/oder beschichtet und/oder imprägniert wird, insbesondere durch Aufbringen und/oder Inkontaktbringen, vorzugsweise Fixierung, der katalytisch aktiven Komponente auf dem Katalysatorträger, gegebenenfalls gefolgt von einer Reduktion ...

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

New heterogeneous ruthenium catalyst comprising amorphous silicon dioxide, useful in the hydrogenation of a carbocyclic aromatic group to the corresponding carbocyclic aliphatic group

Heterogeneous ruthenium catalyst comprising an amorphous silicon dioxide as substrate (obtained by the impregnation of one or more carrier material with a ruthenium salt solution, followed by drying and reduction; and where the silicon dioxide carrier material exhibits a Brunauer-Emmett and Teller surface (BET surface, according to DIN 66131) of 250-400 m 2>/g, a pore volume (according to DIN 66134) of 0.7-1.1 ml/g and a pore diameter (according to DIN 66134) of 6-12 nm), is new. An independent claim is included for the hydrogenation of a carbocyclic aromatic group to the corresponding carbocyclic aliphatic group comprising using heterogeneous ruthenium catalyst.

ALUMINA EXTRUDATES

... 1404017 Alumina extrudates CONTINENTAL OIL CO 2 Aug 1972 [2 Aug 1971 20 Oct 1971 3 July 1972] 36149/72 Heading C1A Alumina extrudates having (a) a surface area of at least 150 m.2/g., (b) a cumulative pore volume (0-10,000 Š) of at least 0À8 cc./g. and (c) a bulk density of not more than 35 lb./ft.3, are obtained by extruding an alumina hydrate and water mixture, wherein the alumina has been prepared from an aluminium alkoxide. The extrudate may have a surface area of up to 400 m.2/g., a pore vol. up to 2À0 cc./g., a bulk density minimum of 15 lb./ft.3 and a diam. of 1/ 32 -“ inch. The alumina hydrate may have a surface area of 250-500 m.2/g., a pore vol. of 0À8-2À5 cc./g., a bulk density of 8-35 lb./ft.3 and an Al 2 O 3 content of 73-100% by wt. The alumina hydrate may be prepared by hydrolysing aluminium alkoxides, produced by the Ziegler process and containing 2-26 carbon atoms in each alkoxide group, separating the aq. phase ...

Hydrogenation catalyst

A hydrogenation catalyst for desulfurization and removal of heavy metals, comprises (a) at least one metal component selected from metals of Groups VI B and VIII of the Periodic Table, as a catalytically active component, and (2) a porous activated alumina carrier obtained by shaping a mixture of carbon black and a powder of activated alumina or a precursor of activated alumina, drying the shaped mixture and firing it in an oxygen-containing gas stream to burn off the carbon black.

CATALYST FOR USE IN HYDROTREATING HEAVY HYDROCARBON OILS METHOD OF PREPARING SAME AND PROCESS FOR HYDROTREATING HEAVY HYDROCARBON OILS

PROCESS FOR PREPARING SPHEROIDAL ALUMINA PARTICLES

PROCESS FOR THE UPGRADING OF HEAVY HYDROCARBON OILS

... 1523343 Hydrogenation of heavy oils SHELL INTERNATIONAL RESEARCH MAATSCHAPPIJ BV 25 Sept 1975 [27 Sept 1974] 39291/75 Heading C5E Heavy hydrocarbon oil having a C 5 -asphaltene content above 5% by weight and a V k210 above 30 cSt is treated, to reduce its C 5 -asphaltene content by at least 30% and its V k210 by at least 50%, by contacting at at least 400‹ C., a hydrogen partial pressure of at least 100 bar and a space velocity of at most 2 1.1-1.h-1 with a catalyst comprising one or more metals having hydrogenation activity on a carrier and which meets the requirements (1) P/d>3À5-0À02 v (p is the specific average pore diameter in nm, d is the specific average particle diameter in mm and v is the percentage of the total pore volume that consists of pores with a diameter larger than 100 nm); (2) the total pore volume is larger than 0.40 ml./g.; (3) v is smaller than 50; (4) the specific surface area is larger than 100 m.2/g.; and (5) if p/d#10-0.15 v then (a) ...

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

VERFAHREN ZUR HERSTELLUNG EINES POROESEN ALUMINIUMOXIDS

PROCEDURE FOR THE PRODUCTION OF A HIGH-ACTIVITY HYDRAULIC DESULPHURISATION CATALYST

PROCEDURE FOR THE PRODUCTION OF A POROUS ALUMINA

COMPOSITION ON THE BASIS OF ALUMINOPHOSPHATE WITH A LARGE PORENVOLUMEN AND A LARGE PORE DIAMETER, PROCEDURE FOR YOUR PRODUCTION AND USE OF IT

AMORPHOUS SILICIC ACID PARTICLES, PROCEDURES FOR THEIR PRODUCTION AND THEIR USE.

PROCEDURE FOR THE PRODUCTION OF LOW ONES OF MULTI-VALUED ALCOHOLS AND NEW CATALYST DUE TO OF RUTHENIUM USABLE FOR THIS PROCEDURE

PROCEDURE FOR THE PRODUCTION OF A KATALYSATORTRÄGERS, A CATALYST AND A PROCEDURE FOR OLEFINPOLYMERISATION

KATALYSATORTRÄGER, CARRIER CATALYSTS, PROCEDURES FOR THEIR PRODUCTION AND THEIR USE

CERIUM OXIDE ALUMINA OF ABSTENTIONS OXIDATION CATALYST AND PROCEDURE FOR APPLICATION.

PROCESS FOR THE PREPARATION OF VINYL ACETATE

Four component polymerization catalyst

Fast activating catalyst

Continuous catalyst activator

Cobalt-based Fischer-Tropsch synthesis catalyst coated with mesoporous materials and preparation method therefor

A cobalt-based Fischer-Tropsch synthesis catalyst coated with mesoporous materials and preparation method therefor are disclosed. The catalyst comprises a silica carrier surface-loaded with an active component of cobalt and a selective promoter of zirconium; the outside of the active component of cobalt and the selective promoter of zirconium is coated with a mesoporous material shell layer. The preparation method comprises preparing silica carrier loaded with zirconium, preparing an initial cobalt-based Fischer-Tropsch synthesis catalyst on the silica carrier base, formulating a precursor solution of mesoporous materials, then dipping, crystallizing, washing, drying and calcining to obtain the cobalt-based Fischer-Tropsch synthesis catalyst coated with mesoporous materials. The active component is coated and protected by the mesoporous material shell layer, the thickness of the shell layer is controllable, the catalyst has long service life, high reactivity and good stability. The pore ...

A catalyst composition

Process for the preparation of a catalyst support, catalyst for olefin polymerization and process for the polymerization of olefins with said catalyst

Rigid porous carbon structures, methods of making, methods of using and products containing same

Hydrothermally stable high pore volume aluminum oxide/swellable clay composites and methods of their preparation and use

CATALYST

PROCESS FOR THE PREPARATION OF NEW CATALYSTS

An invention is a catalyst comprising one or more metals selected from the group consisting of nickel, cobalt, molybdenum and vanadium on a carrier and displaying the following characteristics: (1) the quotient of the specific average pore diameter (p in nm) and the specific average particle diameter (d in nm) is larger than 15, (2) the percentage (v) of the total pore volume that consists of pores with a diameter larger than 100 nm is at least 50, (3) the pore volume (y) that consists of pores with a diameter larger than 50 nm is at least 0.2 ml/g, and (4) the specific surface area is larger than 150 m2/g. The invention also extends to a process for preparing the catalyst. The catalyst is useful in the treatment with hydrogen of heavy oil to demetallize the heavy oil before the heavy oil is subjected to cracking, hydrocracking or hydrodesulphurization.

HYDROGENATION CATALYST FOR DESULFURIZATION AND REMOVAL OF HEAVY METALS

A hydrogenation catalyst for desulfurization and removal of heavy metals, comprises (a) at least one metal component selected from metals of Groups VI A and VIII of the Periodic Table, as a catalytically active component, and (2) a porous activated alumina carrier obtained by shaping a mixture of carbon black and a powder of activated alumina or a precursor of activated alumina, drying the shaped mixture and firing it in an oxygen-containing gas stream to burn off the carbon black.

CATALYST FOR HYDROTREATING HEAVY HYDROCARBON OILS, METHOD OF PREPARING SAME AND PROCESS FOR HYDROTREATING HEAVY HYDROCARBON OILS

Of the Disclosure A catalyst for hydortreating a heavy hydrocarbon oil comprises a carrier which is a calcined composite of a mixture of a clay mineral consisting mainly of magnesium silicate having a doublechain structure and a pseudoboehmite which shows a powder x-ray diffraction spectrum obtained by applying a CuK.alpha. ray such that the half value width of the peak on the (020) plane is between about 0.8.degree. and 4.0.degree. and the intensity of said peak is between 1.2 and 8.0 times as high as that at 2.theta. = 10.degree.. At least one catalytic metal component is composited wiht the carrier, the metal of the catalytic metal componenet being selected from the group consisting of metals belonging to Groups VB, VIB, VIII and IB of the Periodic Table. Disclosed also are a method of preparing such a catalyst, and a process for the hydrotreatment of heavy hydrocarbon oils containing asphaltenes and heavy metals.

HIGH-POROSITY, HIGH-SURFACE AREA, LOW-BULK DENSITY ALUMINA

HYDROPROCESSING CATALYST AND PROCESS FOR HYDROPROCESSING HYDROCARBON FEEDS WITH SAID CATALYST

The invention relates to a spherical catalyst composition comprising a Group VI metal component and optionally a Group VIII metal component on a carrier, which catalyst has a particle size of 0.5-7 mm, a total pore volume of 0.5-1.3 ml/g, an average pore diameter of 15-30 nm, and a %PV(100 nm) of 2-30 %, there being substantially no difference in density between the core region of the carrier particles and their surface regions. The catalyst is particularly suitable for use in non-fixed bed processes for the hydroprocessing of heavy hydrocarbon feeds. It has high hydrodesulphurisation and hydrodemetallisation activity in combination with a high abrasion resistance.

CATALYST FOR HYDROTREATING HEAVY HYDROCARBON OILS, METHOD OF PREPARING SAME AND PROCESS FOR HYDROTREATING HEAVY HYDROCARBON OILS

HYDROTREATING CATALYST AND PROCESS

CARBON MATERIAL FOR CATALYST CARRIER OF POLYMER ELECTROLYTE FUEL CELL, AND METHOD OF PRODUCING THE SAME

A carbon material for a catalyst carrier of a solid polymer fuel cell, the carbon material being a porous carbon material having a three-dimensional tree-shaped structure branched three-dimensionally, wherein the branch diameter is 81 mm or below and the following conditions are satisfied at the same time: (A) the BET specific surface area SBET is 400-1500 m2/g; and (B) in the relationship between the mercury pressure PHg and the mercury absorption amount VHg measured by mercury porosimetry, the amount of increase ?VHg:4.3-4.8 in the mercury absorption amount VHg measured when the common logarithm LogPHg of the mercury pressure PHg increases from 4.3 to 4.8 is 0.82-1.5 cc/g. In addition, a method for manufacturing such a carbon material for a catalyst carrier.

NOBLE METAL HYDROGENATION CATALYSTS AND AROMATIC SATURATION METHODS

Methods are provided for modifying hydrogenation catalysts having silica supports (or other non-alumina supports) with additional alumina, and using such catalysts to achieve unexpectedly superior hydrogenation of feedstocks. The modified hydrogenation catalysts can have a relatively low cracking activity while providing an increased activity for hydrogenation.

PROCESS FOR PRODUCING ALKENES FROM OXYGENATES BY USING SUPPORTED HETEROPOLYACID CATALYSTS

The present invention relates to a supported heteropolyacid catalyst, to a process for producing alkenes from oxygenates in the presence of said catalyst, and to the use of said catalyst in a process for producing alkenes from oxygenates at a higher productivity whilst reducing the formation of alkanes.

SULFUR TOLERANT ALUMINA CATALYST SUPPORT

The present invention is directed to an improved catalyst support and to the resultant catalyst suitable for treating exhaust products from internal combustion engines, especially diesel engines. The support of the present invention is a structure comprising alumina core particulate having high porosity and surface area, wherein the structure has from about 1 to about 8 weight percent silica in the form of cladding on the surface area of said alumina core. The resultant support has a sulfur tolerance efficiency (.eta.) of at least 1000 µg/m2.

COBALT-BASED FISCHER-TROPSCH SYNTHESIS CATALYST COATED WITH MESOPOROUS MATERIALS AND PREPARATION METHOD THEREFOR

A cobalt-based Fischer-Tropsch synthesis catalyst coated with mesoporous materials and preparation method therefor are disclosed. The catalyst comprises a silica carrier surface-loaded with an active component of cobalt and a selective promoter of zirconium; the outside of the active component of cobalt and the selective promoter of zirconium is coated with a mesoporous material shell layer. The preparation method comprises preparing silica carrier loaded with zirconium, preparing an initial cobalt-based Fischer-Tropsch synthesis catalyst on the silica carrier base, formulating a precursor solution of mesoporous materials, then dipping, crystallizing, washing, drying and calcining to obtain the cobalt-based Fischer-Tropsch synthesis catalyst coated with mesoporous materials. The active component is coated and protected by the mesoporous material shell layer, the thickness of the shell layer is controllable, the catalyst has long service life, high reactivity and good stability. The pore ...

NOVEL RESID HYDROTREATING CATALYST

Catalyst supports, supported catalysts, and a method of preparing and using the catalysts for the demetallation of metal-containing heavy oil feedstocks are disclosed. The catalyst supports comprise precipitated alumina prepared by a low temperature pH swing process. A large portion of the pore volume of the catalyst supports has pores with a diameter in the range of about 200 to about 500. Catalysts prepared from the supports of the invention exhibit improved catalytic activity and stability to remove metals from heavy hydrocarbon feedstocks during a hydroconversion process. The catalysts also exhibit increased sulfur and MCR conversion during the hydroconversion process.

METHODS FOR PRODUCING FLUORIDED-CHLORIDED SILICA-COATED ALUMINA ACTIVATOR-SUPPORTS AND CATALYST SYSTEMS CONTAINING THE SAME

Methods for the preparation of fluorided-chlorided silica-coated alumina activator-supports are disclosed. These comprise (a) calcining a silica-coated alumina at a peak calcining temperature to produce a calcined silica-coated alumina; (b) contacting the calcined silica- coated alumina with a chlorine-containing compound and calcining at a peak chloriding temperature to produce a chlorided silica-coated alumina; and (c) contacting the chlorided silica-coated alumina with a fluorine-containing compound and calcining at a peak fluoriding temperature to produce the fluorided-chlorided silica-coated alumina. These activator-supports can be used in catalyst systems further comprising a metallocene compound and optionally a co-catalyst, for the production of olefin-based polymers, such as polyethylene and polypropylene.

AROMATIC HYDROGENATION CATALYSTS AND USES THEREOF

Hydrogenation catalysts for aromatic hydrogenation including an organosilica material support, which is a polymer comprising independent units of a monomer of Formula [Z1OZ2OSiCH2]3 (I), wherein each Z1 and Z2 independently represent a hydrogen atom, a C1-C4 alkyl group or a bond to a silicon atom of another monomer; and at least one catalyst metal are provided herein. Methods of making the hydrogenation catalysts and processes of using, e.g., aromatic hydrogenation, the hydrogenation catalyst are also provided herein.

HIGH ACTIVITY SUPPORTED DISTILLATE HYDROPROCESSING CATALYSTS

Supported metallic catalysts comprised of a Group VIII metal, a Group VIB metal, and an organic additive, and methods for synthesizing supported meta llic catalysts are provided. The catalysts are prepared by a method wherein precursors of both metals are mixed and interacted with at least one organic additive, dried, calcined, and sulfided. The catalysts are used for hydropr ocessing, particularly hydrodesulfurization and hydrodenitrogenation, of hyd rocarbon feedstocks.

AN AMORPHOUS SILICA-ALUMINA COMPOSITION AND A METHOD OF MAKING AND USING SUCH COMPOSITION

Described is a novel amorphous silica-alumina composition having a high ratio of pore volume contained in large pores to pore volume contained in medium to small pores. The amorphous silica-alumina composition also may have the characteristic of a strong aluminum-NMR penta-coordinated peak representing greater than 30% of the total aluminum and a method of making such novel amorphous silica-alumina composition using a pH swing preparation method.

A HYDROPROCESSING CATALYST AND METHODS OF MAKING AND USING SUCH A CATALYST

A method of preparing a hydroprocessing catalyst that may have a high metals loading and has a particularly high activity for hydrodenitrogenation. The method uses several metal impregnations in combination with different intermediate treatment steps so as to provide a catalyst composition that includes a mix of different types of catalytically active sites. The method of the invention allows for the optimization and control of the relative ratio of the different types of active catalyst sites on the catalyst composition in order to give certain desired results and improved catalytic performance. The catalyst composition comprises a one or more active metals or active metal precursors that are incorporated onto a support material.

HYDROPROCESSING CATALYSTS AND METHODS FOR MAKING THEREOF

A method to upgrade heavy oil feedstock using an ebullated bed reactor and a novel catalyst system is provided. The ebullated bed reactor system includes two different catalyst with different characteristics: an expanded catalyst zone contains particulate catalyst having a particle size of greater than 0.65 mm; and a slurry catalyst with average particle size from 1 to 300 µm. The slurry catalyst is provided to the ebullated bed system with the heavy oil feedstock, and entrained in the upflowing hydrocarbon liquid passing through the ebullated bed reaction zone. The slurry catalyst reduces the formation of sediment and coke precursors in the reactor system. In one embodiment, the slurry catalyst is prepared from at least a water-soluble metal precursor, which is pre-sulfided or sulfided in-situ. In another embodiment, the slurry catalyst is prepared from rework materials (catalyst fines).

METHOD FOR PRODUCING LUBRICATING BASE OIL WITH LOW CLOUD POINT AND HIGH VISCOSITY INDEX

A method for producing a lubricating base oil with low cloud point and high viscosity index is provided. The method uses a highly waxy distillate oil having an initial boiling point of 300-460?, a wax content of 5% or more, a pour point of -20? or more and a cloud point of -5? or more as a raw material. The lubricating base oil having a low pour point, a low cloud point and a high viscosity index is produced by pre-hydrorefining, isomerized/asymmetrical cracking and supplementary refining in the presence of hydrogen, with premium naphtha and middle fraction oil being co-produced. The method is characterized mainly in the high yield of heavy base oil, low pour point and the cloud point, and high viscosity and viscosity index of the base oil.

REGENERATION OF SPENT PARAFFIN DEHYDROGENATION CATALYST

There is provided a method for regenerating a spent dehydrogenation catalyst used in the conversion of n-paraffin to olefin. The method comprises method steps for removing the coke by treating the catalyst with an ozone-oxygen stream followed by an oxygen stream. The catalyst is stabilized by passing a nitrogen stream and the stabilized catalyst is rejuvenated by passing an air-nitrogen stream containing a halogenated hydrocarbon. This is followed by reducing the metal oxide in the catalyst by passing hydrogen-nitrogen stream.

PROCESS FOR THE PREPARATION OF EXTRUDATES, EXTRUDATES, AND USE OF THE EXTRUDATES

T 5168 PROCESS FOR THE PREPARATION OF EXTRUDATES, EXTRUDATES, AND USE OF THE EXTRUDATES Process for the preparation of extrudates suitable for use in the manufacture of catalysts or catalyst carriers, especially Fischer-Tropsch catalysts, comprising mulling a mixture of finely divided silica, a water soluble compound derived from a metal selected from group IVb of the Periodic Table and water, the mixture having a solids content of 20 to 50% by weight, and extruding the mixture. After drying and/or calcining, the extrudates may be impreqnated with one or more suitable metal compounds, optionally followed by drying, calcination and/or activation, and used as a catalyst. DO7/T5168FF ...

PROCESS FOR THE PREPARATION OF VINYL ACETATE

The invention relates to a process fox the preparation of vinyl acetate in the gas phase from ethylene, acetic acid and oxygen and/or oxygen-containing gases on a catalyst of palladium and/or compounds thereof, and optionally. in additions gold and/or gold compounds, and, as activators, alkali metal compounds and optionally in addition, cadmium compounds on a support. The support comprises SiO2 or an SiO2-Al2O3 mixture having a surface area of 50-250 m2/g and a pore volume of 0.4-1.2 ml/g, and has a grain size of from 4 to 9 mm. 5 to 20% of the pore volume of the support is farmed by pores having radii of from 200 to 3,000 angstrom and 50 to 90% of the pore volume is formed by pores having radii of from 70 to 100 .ANG.ngstrom.

HYDROCONVERSION CATALYST

HYDROCONVERSION CATALYST A catalyst of use in hydroconversion processes comprises palladium supported on a silica-alumina carrier, which carrier has been prepared from an amorphous silica-alumina starting material having a pore volume of at least 1.0 ml/g. A process for the preparation of the aforementioned catalyst comprises preparing a carrier from an amorphous silica-alumina having a pore volume of at least 1.0 ml/g and impregnating the carrier so-formed with palladium by contacting the carrier with a palladium compound in the presence of a liquid, preferably under acidic conditions. The catalyst is of general use in hydroconversion processes, in particular the preparation of middle distillates by the hydroconversion of hydrocarbons prepared by the Fischer-Tropsch process and the hydroisomerisation of alkanes.

COMPACTS BASED ON PYROGENICALLY-PRODUCED SILICON DIOXIDE

Compacts based on pyrogenically-produced silicon dioxide and having the following physical and chemical characteristics: Outer diameter 0.8 - 20 mm BET surface area 30 - 400 m2/g Pore volume 0.5 - 1.3 ml/g Breaking strength 10 to 250 N Composition > 99.8 wt.% SiO2 Other constituents < 0.2 wt.% Abrasion < 5 wt.% Apparent weight 350 - 750 g/l. are produced by a method in which pyrogenically-produced silicon dioxide is homogenised with methyl cellulose, microwax and polyethylene glycol with addition of water, dried at a temperature of 80 - 150.degree.C and comminuted to a powder, optionally the powder is compressed into compacts, and heat-treated at a temperature of 400 to 1200.degree.C for a time of 0.5 to 8 hours. These compacts can be used as catalysts or catalyst carriers in vinyl acetate monomer production and ethylene hydration.

HYDROCONVERSION PROCESS EMPLOYING A CATALYST WITH SPECIFIED PORE SIZE DISTRIBUTION AND NO ADDED SILICA

A process for hydroconverting a hydrocarbon feed containing components boili ng above 1000 .degree.F (538 .degree.C), sulphur, metals and carbon residue into product containing decreased levels of components having a boiling point greater than 1000 .degree.F (538 .degree.C), decreased levels of sulphur, particularly decreased sulphur contents in the unconverted 1000 .degree.F+ (538 .degree.C+) boiling point products and reduced sediment, which comprises: contacting said hydrocarbon feed with hydrogen at isotherma l hydroprocessing conditions in the presence of, as catalyst, a porous alumina support containing .ltoreq. 0.5 wt.% of silica, no silicon containing components being intentionally added, and bearing 2.2-6 wt.% of a Group VIII metal oxide, 7-24 wt.% of a Group VIB metal oxide and 0 .0- 2.0 wt.% of a phosphorus oxide, said catalyst having a Total Surface Area of 195-230 m2/g, a Total Pore Volume (TPV) of 0.82-98 cc/g, and a Pore Diameter Distribution wherein 27.0-34.0 % of the TPV ...

Verfahren zur Herstellung ungesättigter Nitrile

METHOD OF PRODUCING LUBRICATING BASE OIL WITH LOW TEMPERATURE CLOUD AND HIGH VISCOSITY INDEX

КАТАЛИЗАТОР ГИДРООЧИСТКИ, СОДЕРЖАЩИЙ ФОСФОР И БОР

Катализатор, содержащий по меньшей мере один металлический компонент группы VIB, по меньшей мере один металлический компонент группы VIII, фосфорсодержащий и борсодержащий носители. Количество фосфора составляет по меньшей мере 1 мас.% в пересчете на оксид (Р2О5) от общего веса катализатора и количество бора находится в диапазоне от приблизительно 1 до 13 мас.% в пересчете на оксид (В2О3) от общего веса катализатора. В одном из вариантов осуществления изобретения борсодержащий носитель является продуктом совместной экструзии, по меньшей мере, носителя и источника бора. Кроме того, описан способ изготовления катализатора и его использование для гидроочистки углеводородного сырья.

НАСЫПНОЙ КАТАЛИЗАТОР ГИДРОГЕНИЗАЦИИ И ЕГО ПРИМЕНЕНИЕ

Предоставлен насыпной катализатор гидрогенизации. Также предоставлен способ получения насыпных катализаторов гидрогенизации. Кроме того, предоставлено применение насыпного катализатора при гидрогенизации нефтяного сырья. Катализатор гидрогенизации имеет формулу (Mt)a(Lu)b(Sv)d(Cw)e(Hx)f(Oy)g(Nz)h, где М - по меньшей мере один из металлов группы VIB; металлический промотор L является опциональным компонентом, и если он присутствует, то L - по меньшей мере один из неблагородных металлов группы VIII; t, u, v, w, х, у, z представляют собой общий заряд для каждого из компонентов (М, L, S, С, Н, О и N, соответственно); ta+ub+vd+we+xf+yg+zh=0; 0≤b и 0≤b/a≤5, (а+0,5b)≤d≤(5a+2b), 0≤е≤11(a+b), 0≤f≤7(a+b), 0≤g≤5(a+b), 0≤h≤0,5(a+b). Катализатор имеет картину рентгеновской порошковой дифракции с по меньшей мере одним широким дифракционным пиком при любом из следующих брэгговских углов: от 8 до 18°, от 32 до 40° и от 55 до 65° (от 0 до 70° по оси 2-θ). В одном из вариантов осуществления катализатор получают ...

СИНТЕЗ МИКРОПОРИСТОГО СИЛИКАГЕЛЯ И ЕГО ПРИМЕНЕНИЕ ДЛЯ ПРИГОТОВЛЕНИЯ КАТАЛИЗАТОРОВ ДЛЯ СИНТЕЗА C2-ОКСИГЕНАТОВ ИЗ СИНТЕЗ-ГАЗА

Предложен синтез микропористого силикагеля и его применение для приготовления катализаторов для синтеза С2-оксигенатов из синтез-газа. Мелкие частицы силикагеля, которые получают золь-гель методом, нагревают в основном растворе, затем сушат и/или прокаливают, и таким образом образуется микропористый оксид кремния для применения в качестве носителя для катализаторов. Основной раствор может представлять собой раствор отдельной соли или смешанный раствор гидроксидов, карбонатов, бикарбонатов, формиатов и ацетатов щелочного металла и аммония. Полученный микропористый оксид кремния можно пропитать растворами соли родия и солей других переходных элементов (в качестве предшественников промотора), а затем высушить и/или прокалить, таким образом получается микропористый нанесенный на оксид кремния катализатор на основе родия. Соль родия может представлять собой RhCl3 или Rh(NO3)3. Предшественники промотора могут представлять собой растворимые в воде соли переходного металла, соли редкоземельных ...

Process for hydrodesulphurizing gasoline cuts containing sulphur and olefins in the presence of a catalyst

Composition containing oxides of zirconium, cerium and at least one other rare earth and having a specific porosity, method for preparing same and use thereof in catalysis

The invention relates to a composition that contains zirconium oxide, cerium oxide and yttrium oxide, or zirconium oxide, cerium oxide and at least two oxides of two rare earths different from cerium in a mass proportion of at least 20 % of zirconium oxide and of at most 70 % of cerium oxide, characterized in that said composition comprises, after calcination at 900 DEG C for 4 hours, two populations of pores having respective diameters centered, for the first population, about a value of between 20 and 40 nm and, for the second, about a value of between 80 and 200 nm. The composition can be used for processing exhaust gases of internal combustion engines.

Catalyst, method for producing the same, and method for producing chlorine using the catalyst

From the hydrocarbon feedstock of arsenic from method

CATALYST COMPRISING GOLD DISPERSED HOMOGENEOUSLY IN A POROUS SUPPORT

Catalyseur comprenant de l'or et un support poreux contenant au moins un oxyde réfractaire, dans lequel la teneur en or est comprise entre 0,01 et 5 % poids par rapport au poids total du catalyseur, et dans lequel les particules d'or sont réparties de manière homogène à travers dudit support poreux et présente une taille mesurée par microscopie électronique à transmission comprise entre 0,5 et 5 nm.

PROCESS FOR the PREPARATION OF NEW CATALYSTS AND APPLICATION OF THESE CATALYSTS TO the TREATMENT BY the HYDROCARBON OIL HYDROGEN

HEAVY CRUDE CONVERSION CATALYSTS THEREFOR AND THEIR PREPARATION

Paraffin alkylation catalyst.

POROUS PRODUCT OUT OF REFRACTORY MINERAL OXIDE, ITS METHOD OF PREPARATION AND ITS APPLICATION LIKE CATALYST OR CATALYST SUPPORT

CATALYST INVOLVING A SILICE-ALUMINE AND ITS USE IN HYDROCRAQUAGEDE HYDROCARBON LOADS

PROCESS Of HYDROCONVERSION IN SLURRY OF HEAVY HYDROCARBON LOADS IN THE PRESENCE OF an ACTIVE PHASE DISPERSEE AND Of an OXIDE CONTAINING ALUMINA.

AMMOXIDATION CATALYST FOR PROPYLENE, MANUFACTURING METHOD OF THE SAME CATALYST, AMMOXIDATION METHOD USING THE SAME CATALYST

There are provided an ammoxidation catalyst for propylene, a manufacturing method of the same, and an ammoxidation method of propylene using the same. Specifically, according to one embodiment of the invention, there is provided an ammoxidation catalyst for propylene that not only exhibits high activity to ammoxidation of propylene, but also has high amorphous phase content. 1. An ammoxidation catalyst for propylene comprising metal oxide represented by the following Chemical Formula 1 ,wherein a first peak having intensity of A appears in the 2θrange of 26.3±0.5°, and a second peak having intensity of B appears in the 2θrange of 28.3±0.5° in X ray diffraction analysis by CuKα, and {'br': None, 'sub': x', 'a', 'b', 'c', 'd', 'e', 'f', 'y, 'MoBiFeABCDO\u2003\u2003[Chemical Formula 1]'}, 'a intensity ratio(AB) of the first peak to the second peak is 1.5 or morein the Chemical Formula 1,A and B are different from each other, and each independently, are one or more elements of Ni, Mn, Co, Zn, Mg, Ca, and Ba,C is one or more elements of Li, Na, K, Rb, and Cs,D is one or more elements of Cr, W, B, Al, Ca, and V,a to f, x, and y are respectively mole fractions of each atom or atomic group,a is 0.1 to 7, b is 0.1 to 7, provided that the sum of a and b is 0.1 to 7,c is 0.1 to 10, d is 0.01 to 5, e is 0.1 to 10, f is 0 to 10,x is 11 to 14, y is a value determined by each oxidation number of Mo, Bi, Fe, A, B, C, and D.2. The ammoxidation catalyst for propylene according to claim 1 , wherein the intensity ratio(AB) is 3.0 or more.3. The ammoxidation catalyst for propylene according to claim 1 , wherein the catalyst has BET specific surface area of 50 to 300 m/g.4. The ammoxidation catalyst for propylene according to claim 1 , wherein a pore volume in the catalyst is 0.3 to 1.3 cm/g.5. The ammoxidation catalyst for propylene according to claim 1 , wherein the metal oxide is represented by Chemical Formula 1-1:{'br': None, 'sub': x', 'a', 'b', 'c', 'd', 'e', 'y, 'MoBiFeNiCoKO\ ...

INORGANIC OXIDE MATERIAL

The present teachings are directed to inorganic oxide materials that include AlO, CeO, and at least one of MgO and PrO. The present teachings are also directed to catalysts having at least one noble metal supported on these inorganic oxide materials, as well as methods for treating exhaust gases from internal combustion engines using such catalysts. 1. An inorganic oxide material , comprising:{'sub': 2', '3, '(a) from about 25 to about 90 pbw AlO;'}{'sub': '2', '(b) from about 5 to about 35 pbw CeO;'}(c)(i) from about 5 to about 35 pbw MgO, or{'sub': 6', '11, '(c)(ii) from about 2 to about 20 pbw PrO, or'}{'sub': 6', '11, '(c)(iii) from about 5 to about 35 pbw MgO, and from about 2 to about 20 pbw PrO; and'}(d) optionally up to about 10 pbw of a combined amount of oxides of one or more dopants selected from transition metals, rare earths, and mixtures thereof.2. The inorganic oxide material of claim 1 , wherein the material comprises from about 40 to about 80 pbw AlOand from about 10 to about 30 pbw CeO.3. (canceled)4. The inorganic oxide material of claim 1 , wherein the material comprises from about 10 to about 30 pbw MgO.5. The inorganic oxide material of claim 1 , wherein the material comprises from about 5 to about 15 pbw PrO.6. The inorganic oxide material of claim 1 , wherein the material comprises from about 10 to about 30 pbw MgO and from about 5 to about 15 pbw PrO.7. The inorganic oxide material of claim 1 , wherein the material comprises from about 1 to about 10 pbw of an oxide or a mixture of oxides selected from YO claim 1 , LaO claim 1 , NdOand GdO.8. The inorganic oxide material of claim 1 , wherein the material comprises from about 1 to about 4 pbw LaO.9. The inorganic oxide material of claim 1 , wherein the material comprises (a) crystallites comprising AlOand at least one oxide selected from MgO and PrO claim 1 , and (b) crystallites comprising CeO.11. The inorganic oxide material of claim 10 , wherein the material comprises from about 40 to about ...

PROPYLENE PRODUCTION USING A MESOPOROUS SILICA FOAM METATHESIS CATALYST

Embodiments of a metathesis process for producing propylene comprise providing a metathesis catalyst comprising an amorphous mesoporous silica foam impregnated with metal oxides, where the metathesis catalyst has a pore size distribution of at least 3 nm to 40 nm and a total pore volume of at least 0.700 cm/g. The process further involves producing a product stream comprising propylene by contacting a feed stream comprising butene with the metathesis catalyst. 1. A metathesis process for producing propylene comprising:{'sup': '3', 'providing a metathesis catalyst comprising an amorphous mesoporous silica foam impregnated with metal oxides, where the metathesis catalyst has a pore size distribution of at least 3 nm to 40 nm and a total pore volume of at least 0.700 cm/g; and'}producing a product stream comprising propylene by contacting a feed stream comprising butene with the metathesis catalyst.2. The process of further comprising tri-block copolymer structuring agent claim 1 , where the tri-block copolymer structuring agent is poly(ethylene glycol)-block-poly(propylene glycol)-block-poly(ethylene glycol) structure.3. The process of where the metathesis catalyst catalyzes isomerization of 2-butene to 1-butene followed by cross-metathesis of 2-butene and 1-butene into a metathesis product stream comprising propylene4. The process of where at least 90% of the 2-butene is converted to 1-butene via isomerization.5. The process of where the pore size distribution is from at least 4 nm to 10 nm and the total pore volume is from at least 0.800 cm/g to 1.5 cm/g.6. The process of where the metathesis catalyst has a total acidity from 0.125 mmol/g to 0.500 mmol/g claim 1 , and a surface area of 400 to 500 m/g.7. The process of where the metal oxide is an oxide of molybdenum claim 1 , rhenium claim 1 , tungsten claim 1 , or combinations thereof.8. The process of where the metal oxide is tungsten oxide.9. The process of where the metathesis catalyst has a molar ratio for ...

SYSTEMS AND METHODS FOR PRODUCING PROPYLENE

According to one embodiment described in this disclosure, a process for producing propylene may comprise at least partially metathesizing a first stream comprising at least about 10 wt. % butene to form a metathesis-reaction product, at least partially cracking the metathesis-reaction product to form a cracking-reaction product comprising propylene, and at least partially separating propylene from the cracking-reaction product to form a product stream comprising at least about 80 wt. % propylene. 1. A process for producing propylene , the process comprising:{'sup': '3', 'at least partially metathesizing a first composition comprising at least 10 wt. % butene to form a metathesis-reaction product, where the first composition is metathesized with a metathesis catalyst comprising a mesoporous silica catalyst impregnated with metal oxide, where the mesoporous silica catalyst includes a pore size distribution of about 2.5 nm to about 40 nm and a total pore volume of at least about 0.600 cm/g;'}at least partially cracking the metathesis-reaction product to form a cracking-reaction product comprising propylene, where the metathesis-reaction product is cracked with a cracking catalyst comprising a mordenite framework inverted (MFI) structured silica catalyst, where the MFI structured silica catalyst includes total acidity of 0.001 mmol/g to 0.1 mmol/g; andat least partially separating propylene from the cracking-reaction product to form a product composition comprising at least 80 wt. % propylene.2. The process of claim 1 , where the MFI structured silica catalyst has a pore size distribution of at least 1.5 nm to 3 nm.3. The process of claim 1 , where the MFI structured silica catalyst is free of acidity modifiers selected from the group consisting of rare earth modifiers claim 1 , phosphorus modifiers claim 1 , potassium modifiers claim 1 , and combinations thereof.4. The process of claim 1 , where the metathesis catalyst is positioned generally upstream of the cracking ...

DUAL CATALYST SYSTEM FOR PROPYLENE PRODUCTION

Embodiments of processes for producing propylene utilize a dual catalyst system comprising a mesoporous silica catalyst impregnated with metal oxide and a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm/g, and the MFI structured silica catalyst has a total acidity of 0.001 mmol/g to 0.1 mmol/g. The propylene is produced from the butene stream via metathesis by contacting the mesoporous silica catalyst and subsequent cracking by contacting the MFI structured silica catalyst. 1. A process for production of propylene comprising: [{'sup': '3', 'a mesoporous silica catalyst impregnated with metal oxide, where the mesoporous silica catalyst includes a pore size distribution of about 2.5 nm to about 40 nm and a total pore volume of at least about 0.600 cm/g, and'}, 'a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the MFI structured silica catalyst includes a total acidity of 0.001 mmol/g to 0.1 mmol/g,, 'providing a dual catalyst system comprisingproducing propylene from a stream comprising butene via metathesis and cracking by contacting the stream comprising butene with the dual catalyst system, where the stream comprising butene contacts the mesoporous silica catalyst before contacting the MFI structured silica catalyst.2. The process of where the MFI structured silica catalyst has a pore size distribution of at least 1.5 nm to 3 nm.3. The process of where the MFI structured silica catalyst is free of acidity modifiers selected from the group consisting of rare earth modifiers claim 1 , phosphorus modifiers claim 1 , potassium modifiers claim 1 , and combinations thereof.4. The process of where the mesoporous silica catalyst catalyzes isomerization of 2-butene to 1-butene followed by cross-metathesis of ...

Synthesis of fibrous nano-silica spheres with controlled particle size, fibre density, and various textural properties

The present disclosure provides a method for synthesizing fibrous silica nanospheres, the method can include, in sequence, the steps of: a) providing a reaction mixture comprising a silica precursor, a hydrolyzing agent, a template molecule, a cosurfactant and one or more solvents; b) maintaining the reaction mixture under stirring for a length of time; c) heating the reaction mixture to a temperature for a length of time; d) cooling the reaction mixture to obtain a solid, and (e) calcinating the solid to pro duce fibrous silica nanospheres, wherein desirable product characteristics such as particle size, fiber density, surface area, pore volume and pore size can be obtained by controlling one or more parameters of the method. The present disclosure further provides a method for synthesizing fibrous silica nanospheres using conventional heating such as refluxing the reactants in an open reactor, thereby eliminating the need for microwave heating in a closed reactor or the need for any pressure reactors.

PROCESSING OF HEAVY HYDROCARBON FEEDS

Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude. 1. A process for producing a hydroprocessed product , comprising:exposing a feedstock to a catalyst under effective slurry hydroconversion conditions to form a slurry hydroprocessing effluent, the effective slurry hydroconversion conditions being effective for conversion of at least about 90 wt % of the feedstock relative to a conversion temperature, the catalyst comprising catalyst particles having a particle size of at least about 2 μm; andseparating at least about 95 wt % of the catalyst particles having a particle size of at least about 2 μm from the slurry hydroprocessing effluent using a catalyst recovery system comprising one or more drum separators and a cross-flow filter.2. The process of claim 1 , wherein the feedstock has a T95 distillation point of about 600° C. or less.3. The process of claim 1 , wherein the feedstock has a 10% distillation point of at least about 900° F. (˜482° C.) claim 1 , a Conradson carbon residue of at least about 27.5 wt % claim 1 , or a combination thereof.4. The process of claim 1 , wherein the one or more drum separators comprise cyclone separators.5. The process of claim 1 , further comprising exposing the feedstock to a demetallization catalyst under slurry ...

Oxygen reduction reaction catalyst

A method for the manufacture of an oxygen reduction reaction (ORR) catalyst, the method comprising; providing a metal organic framework (MOF) material having a specific internal pore volume of 0.7 cm 3 g −1 or greater; providing a source of iron and/or cobalt; pyrolysing the MOF material together with the source of iron and/or cobalt to form the catalyst, wherein the MOF material comprises nitrogen and/or the MOF material is pyrolysed together with a source of nitrogen and the source of iron and/or cobalt is disclosed.

A CATALYST AND ITS USE IN FATTY ACID ISOMERISATION

The present invention relates to an isomerisation catalyst, in particular a zeolite catalyst. There is provided a method for making a particularly preferred zeolite catalyst by means of modifying catalytic zeolite materials. There is also provided a 5 process for isomerising fatty acids or alkyl esters thereof to produce branched fatty acids employing such an isomerisation catalyst, a composition comprising branched fatty acids, and also use of the isomerisation catalyst. 1. An isomerisation catalyst , wherein: {'br': None, 'i': 'S', 'sub': external', '3, 'activity factor=×strong NHuptake\u2003\u2003(I)'}, 'the catalyst has an activity factor of from 30,000 to 200,000, wherein the activity factor is calculated as shown in formula (I)wherein:{'sub': 'external', 'sup': '2', '“S” is the external surface area in m/g of the catalyst, measured by nitrogen physisorption; and'}{'sub': 3', '3, '“strong NHuptake” is the amount of NHin μmol/g which desorbs from the catalyst at a temperature between 327° C. and 550° C. during ammonia temperature programmed desorption.'}2. (canceled)3. A catalyst according to claim 1 , wherein said catalyst is a zeolite or zeotype material.4. A catalyst according to claim 3 , wherein said catalyst is a zeolite of the MFI type framework.5. A catalyst according to claim 3 , wherein said catalyst is a zeolite and comprises channels with 10 member ring structures.6. A catalyst according to claim 3 , wherein said catalyst is a ZSM-5 zeolite.7. A catalyst according to claim 1 , wherein the catalyst has Sof at least 80 m/g.8. A catalyst according to claim 1 , wherein the catalyst has strong NHuptake of at least 100 μmol/g.9. A catalyst according to claim 1 , which has a silica to alumina molar ratio (SAR) of at least 15.10. A catalyst according to claim 3 , wherein the zeolite is suitable for use as an isomerisation catalyst claim 3 , and wherein the zeolite is obtainable by claim 3 , preferably obtained by claim 3 , a method of modifying the structure ...

POROUS BODIES WITH ENHANCED PORE ARCHITECTURE

A porous body is provided with enhanced fluid transport properties that is capable of performing or facilitating separations, or performing reactions and/or providing areas for such separations or reactions to take place. The porous body includes at least 80 percent alpha alumina and has a pore volume from 0.3 mL/g to 1.2 mL/g and a surface area from 0.3 m/g to 3.0 m/g. The porous body further includes a pore architecture that provides at least one of a tortuosity of 7.0 or less, a constriction of 4.0 or less and a permeability of 30 mdarcys or greater. The porous body can be used in a wide variety of applications such as, for example, as a filter, as a membrane or as a catalyst carrier. 1. A precursor mixture for producing a porous body , the precursor mixture comprising:(i) at least one milled alpha alumina powder having a particle size of 0.1 microns to 6 microns,(ii) a non-silicate binder, and(iii) at least one principle burnout material having a particle size of 1 micron to 10 microns.2. The precursor mixture of claim 1 , wherein the least one milled alpha alumina powder claim 1 , the non-silicate binder claim 1 , and the at least one principle burnout material are in a homogeneous mixture.3. The precursor mixture of claim 1 , wherein the at least one principle burnout material is a granulated polyolefin.4. The precursor mixture of claim 3 , wherein the granulated polyolefin is one of polyethylene and polypropylene.5. The precursor mixture of claim 1 , further comprising unmilled alpha alumina powder.6. The precursor mixture of claim 5 , wherein the unmilled alpha alumina powder has an average particle size from 10 microns to 100 microns.7. The precursor mixture of claim 5 , wherein a weight ratio of the milled alpha alumina powder to the unmilled alpha alumina powder is from about 0.25:1 to 5:1.8. The precursor mixture of claim 5 , further comprising an additional unmilled alpha alumina powder having a particle size greater the particle size of the unmilled ...

HYDROPROCESSING CATALYST AND HYDROPROCESSING CATALYST OF MAKING THE SAME

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

Middle distillate hydrocracking catalyst

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

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

Disclosed are processes for conversion of a feedstock comprising C aromatic hydrocarbons to lighter aromatic products in which the feedstock and optionally hydrogen are contacted in the presence of a first and a second catalyst composition under conversion conditions effective to produce said lighter aromatic products comprising benzene, toluene and xylene. In the process, the C aromatic hydrocarbons are dealkylated to form C-Caromatic hydrocarbon and the C olefins formed are saturated. The remaining C aromatic hydrocarbons are transalkylated with the C-Caromatic hydrocarbon. The first and second catalyst compositions each comprise a zeolite, a first metal, and optionally a second metal, and are treated with a source of sulfur and/or a source of steam. 125.-. (canceled)27. The process of claim 26 , wherein said first catalyst composition and/or said second catalyst composition is treated with said source of sulfur in one or more stages at temperatures in the range 204° C. (400° F.) up to about 480° C. (900° F.).28. The process of claim 26 , wherein said source of sulfur is one or more of hydrogen sulfide claim 26 , carbon disulfide and alkylsulfides which are selected from the group consisting of methylsulfide claim 26 , dimethylsulfide claim 26 , dimethyldisulfide claim 26 , diethylsulfide claim 26 , dibutyl sulfide claim 26 , and mixtures of two or more thereof.29. The process of claim 26 , wherein said first zeolite and/or said second zeolite are treated with a source of steam.30. The process of claim 26 , wherein said source of steam comprises up to about 100% steam at temperatures in the range of about 260° C. (500° F.) to about 649° C. (1200° F.) and said treatment is in one or more temperature stages.31. The process of claim 26 , wherein said first metal of Group 6 is selected from the group consisting of chromium claim 26 , molybdenum claim 26 , tungsten and mixtures of two or more thereof.32. The process of claim 26 , wherein said second metal of Group 9 is ...

ACTIVATED CARBON WITH A SPECIAL FINISHING, PRODUCTION AND USE THEREOF

The invention relates to a method for producing activated carbon provided and/or impregnated with a metal-organic framework substance (MOF material), the activated carbon being in particular in the form of discrete activated carbon particles, and preferably for producing an activated carbon with a reactive and/or catalytic action. The metal-organic framework substance is produced in situ in the pores and/or in the pore system of the activated carbon, starting from at least one metal precursor compound(MP) containing a metal and at least one ligand precursor (LP). 1. A process for producing an activated carbon , particularly in the form of discrete particles of activated carbon , endowed and/or impregnated with at least one metal-organic framework substance (MOF material) , preferably for producing an activated carbon having reactive and/or catalytic activity and/or additization ,wherein the metal-organic framework substance is produced and/or formed in situ in the pores and/or the porous system of the activated carbon from at least one metal precursor (MP) compound, which contains at least one metal, and from at least one ligand precursor (LP).2. The process as claimed in wherein the metal-organic framework substance (MOF material) is formed in the pores and/or porous system in at least partially crystalline form claim 1 , preferably in crystalline form.3. The process as claimed in orwherein the metal precursor (MP) compound includes at least one metal, in particular metal atom or metal ion, wherein the metal is selected from elements of groups Ia, IIa, IIIa, IVa, Va, VIa, VIIa, VIIIa, Ib, IIb, IIIb, IVb, Vb and VIb of the periodic table; and/orwherein the metal, in particular metal atom, of the metal precursor (MP) compound is selected from the group of Mg, Ca, Sr, Ba, Sc, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Re, Fe, Ru, Os, Co, Rh, Ir, Ni, Pd, Pt, Cu, Ag, Au, Zn, Cd, Hg, Al, Ga, In, Tl, Si, Ge, Sn, Pb, As, Sb and Bi, preferably selected from the group of Zn, ...

MESOPOROUS MATERIAL-COATED COBALT-BASED CATALYST FOR FISCHER-TROPSCH SYNTHESIS AND METHOD FOR PREPARING THE SAME

A catalyst including cobalt, a carrier including silica, and a selective promoter including zirconium. The cobalt and the selective promoter are disposed on the surface of the carrier, and the outer surfaces of the active component cobalt and the selective promoter zirconium are coated with a shell layer including a mesoporous material. A method for preparing the catalyst, including: 1) soaking the carrier including silica into an aqueous solution including a zirconium salt, aging, drying, and calcining a resulting mixture to yield a zirconium-loaded carrier including silica; 2) soaking the zirconium-loaded carrier including silica into an aqueous solution including a cobalt salt, aging, drying, calcining a resulting mixture to yield a primary cobalt-based catalyst; 3) preparing a precursor solution of a mesoporous material; and 4) soaking the primary cobalt-based catalyst into the precursor solution of the mesoporous material; and crystalizing, washing, drying, and calcining a resulting mixture. 1. A catalyst , comprising:cobalt;a carrier comprising silica; anda selective promoter comprising zirconium;whereinthe cobalt and the selective promoter comprising zirconium are disposed on a surface of the carrier comprising silica; andouter surfaces of the active component cobalt and the selective promoter zirconium are coated with a shell layer comprising a mesoporous material.2. The catalyst of claim 1 , wherein the shell layer comprising the mesoporous material is coated with a hydrophobic organic layer.3. The catalyst of claim 1 , wherein the carrier comprising silica is an inorganic silica gel.4. The catalyst of claim 3 , wherein the inorganic silica gel has a specific area of between 150 and 350 m/g claim 3 , an average pore size of between 3 and 50 nm claim 3 , a pore volume of between 0.7 and 1.7 mL/g claim 3 , and a particle size of between 20 and 200 μm.5. The catalyst of claim 4 , wherein the specific area of the inorganic silica gel is between 200 and 300 m/g ...

Selective catalyst for hydrogenolysis of ethyl-aromatics by conserving methyl-aromatics

The present invention relates to a hydrogenolysis process wherein a hydrocarbon-based feedstock comprising aromatic compounds having at least 8 carbon atoms is treated by means of a hydrogen feed and in the presence of a catalyst, in order to convert C2+ alkyl chains of said aromatic compounds into methyl groups and to produce a hydrogenolysis effluent enriched in methyl-substituted aromatic compounds, wherein the catalyst comprises a support, comprising at least one refractory oxide, and an active phase comprising nickel and molybdenum, wherein: the nickel content being between 0.1 and 25% by weight relative to the total weight of the catalyst; the molybdenum content being between 0.1 and 20% by weight relative to the total weight of the catalyst; and the catalyst comprising a molar ratio of molybdenum to nickel of between 0.2 and 0.9. The present invention also relates to said catalyst and to the process for preparing said catalyst.

NOx Trap Catalyst Support Material Composition

The present invention relates to a method of making a support material composition comprising an Mg/Al oxide, a cerium oxide and at least another rare earth element oxide, to a support material composition and to the use of the support material composition as a nitrogen oxide storage component within a catalyst for treating exhaust gases to reduce NOx content. 1. A method of preparing a support material composition , the composition comprising two phases:a first phase comprising a Mg/Al mixed oxide; anda second phase comprising a cerium based oxide, and rare-earth element(s) based oxide other than cerium oxide, wherein the second phase is a solid-solution; the method comprising the following steps:i) preparing an aqueous suspension of a Mg/Al mixed oxide precursor;ii) preparing an aqueous solution of a cerium salt;iii) preparing an aqueous solution of one or more rare-earth element oxides salt(s) other than cerium salts;iv) combining, in any order, at least the aqueous suspension in step i), with the aqueous solution in step ii), and the aqueous solution of step iii) to form an aqueous mixture;v) dying the aqueous mixture to form a dried particulate material; andvi) calcining the dried particulate material; the cerium salts from the aqueous solution of step ii) and', 'the rare earth element salt(s) other than cerium salts from the aqueous solution of step iii) and,, 'wherein the content of the one or more rare-earth element salt(s) other than cerium is between 5 and 50 wt. %, relative to the sum of'}wherein each of the salts are calculated as their oxides.2. The method of claim 1 , wherein the Mg/Al mixed oxide precursor is prepared by hydrolysis of a mixture of corresponding alkoxides of aluminium and magnesium that form a mixture of hydrotalcite claim 1 , boehmite claim 1 , and water.3. The method of claim 1 , wherein the cerium salt comprises one or more of cerium nitrate claim 1 , ammonium cerium nitrate claim 1 , cerium sulfate claim 1 , cerium carbonate claim ...

METAL CATALYSTS WITH LOW -ALKALI METAL CONTENT AND ACID/METAL BIFUNCTIONAL CATALYST SYSTEMS THEREOF

Methods of producing metal catalysts can include mixing two or more metal salts and an aluminum salt in water to produce a metal catalyst precursor solution; mixing the metal catalyst precursor solution and an alkali metal buffer solution to produce a precipitate; ion exchanging the alkali metal in the precipitate for a non-alkali cation to produce a low-alkali metal precipitate comprising 3 wt % or less alkali metal by weight of the precipitate on a dry basis; producing a powder from the low-alkali metal precipitate; and calcining the powder to produce a metal catalyst. Such metal catalysts may be useful in producing bifunctional catalyst systems that are useful in, among other things, converting syngas to dimethyl ether in a single reactor 1. A method comprising:mixing two or more metal salts and an aluminum salt in water to produce a metal catalyst precursor solution;mixing the metal catalyst precursor solution and an alkali metal buffer solution to produce a precipitate;ion exchanging the alkali metal in the precipitate for a non-alkali cation to produce a low-alkali metal precipitate comprising 3 wt % or less alkali metal by weight of the precipitate on a dry basis;producing a powder from the low-alkali metal precipitate; andcalcining the powder to produce a metal catalyst.2. The method of claim 1 , wherein ion exchanging comprises contacting the precipitate with the non-alkali cation.3. The method of claim 1 , wherein ion exchanging comprises dialysis.4. The method of claim 1 , wherein ion exchanging comprises electrochemical ion exchange.5. The method of claim 1 , wherein producing the powder from the low-alkali metal precipitate comprises:washing the low-alkali metal precipitate;drying the low-alkali metal precipitate; andgrinding the low-alkali metal precipitate, wherein the powder comprises 5 wt % or less of the water.6. The method of claim 1 , wherein the alkali metal buffer solution is at 40° C. to 90° C. when mixing with the metal catalyst precursor ...

ACID/METAL BIFUNCTIONAL CATALYSTS PRODUCED BY SLURRY METHODS

A method of producing a acid/metal bifunctional catalyst may include: mixing an acid catalyst, a metal catalyst, and a fluid to produce a slurry, wherein the acid catalyst is present at 50 wt % or less relative to a total catalyst weight in the slurry; heating the slurry; producing a powder from the slurry; and calcining the powder to produce the acid/metal bifunctional catalyst. Such acid/metal bifunctional catalyst would be useful in the direct conversion of syngas to dimethyl ether as well as other reactions. 1. A method comprising:mixing an acid catalyst, a metal catalyst, and a fluid to produce a slurry, wherein the acid catalyst is present at 50 wt % or less relative to a total catalyst weight in the slurry;heating the slurry;drying the slurry produce a dried slurry;producing a powder from the dried slurry; andcalcining the powder to produce an acid/metal bifunctional catalyst.2. The method claim 1 , wherein producing the powder from the dried slurry comprises:grinding the dried slurry to produce a powder, wherein the powder comprises 5 wt % or less of the fluid.3. The method of claim 1 , wherein mixing is maintained during heating.4. The method of claim 1 , wherein mixing is performed for 30 minutes to 3 hours.5. The method of claim 1 , wherein heating is to a temperature within 20° C. of a boiling point of the fluid.6. The method of claim 1 , wherein the acid catalyst is selected from the group consisting of a zeolite claim 1 , an ion exchanged zeolite claim 1 , a molecular sieve claim 1 , a metal oxide claim 1 , and any combination thereof.7. The method of claim 1 , wherein the metal catalyst is a M1/M2/Al catalyst claim 1 , wherein M1 is selected from the group consisting of Cu claim 1 , Cr claim 1 , Ag claim 1 , Au claim 1 , Ru claim 1 , Rh claim 1 , Pd claim 1 , Re claim 1 , Os claim 1 , Ir claim 1 , Pt claim 1 , and any combination thereof claim 1 , wherein M2 is selected from the group consisting of Ti claim 1 , V claim 1 , Cr claim 1 , Mn claim 1 , Fe ...

Process for Production of Attrition Stable Granulated Material

The present invention relates to granulated particles with improved attrition and a method for producing granulated particles by fluidized bed granulation of inorganic particles wherein particles of reduced particle size are fed into a fluldized-bed granulation reactor thereby producing granulated particles with improved attrition. 1. A method of producing granulated particles in a fluidized-bed granulation reactor , the method comprising feeding inorganic particles dispersed in a dispersion medium into the fluidized-bed granulation reactor , the inorganic particles in the dispersion medium having a Dvalue of between 1 μm and 15 μm.2. The method of wherein the dispersion medium comprising inorganic particles dispersed therein is sprayed into a process chamber of the fluidized-bed granulation reactor while heated process gas flows through the process chamber from the bottom to the top.3. The method of claim 1 , wherein the Dvalue of the inorganic particles in the dispersion medium fed into the fluidized-bed granulation reactor is between 1 μm and 10 μm.4. The method of claim 1 , wherein the inorganic particles include compounds of alkaline earth metals claim 1 , rare earth elements claim 1 , platinum group elements claim 1 , iron group elements claim 1 , Cu claim 1 , Ag claim 1 , Au claim 1 , Zn claim 1 , Al claim 1 , In claim 1 , Sn claim 1 , Si claim 1 , P claim 1 , V claim 1 , Nb claim 1 , Mo claim 1 , W claim 1 , Mn claim 1 , Re claim 1 , Ti claim 1 , Zr or mixtures thereof.5. The method of claim 1 , wherein the inorganic particles are particles of alumina claim 1 , silica claim 1 , or a mixture thereof.6. The method of claim 1 , wherein the dispersion medium comprises water or consists of water.7. The method of claim 1 , wherein a stabilizer is added to the dispersion medium.8. The method of claim 1 , including the initial step of milling the inorganic particles in the dispersion medium to a Dvalue between 1 μm and 15 μm before entering into the fluidized-bed ...

HYDROCRACKING CATALYST, PROCESS FOR PREPARING THE SAME AND USE THEREOF

The present invention relates to a hydrocracking catalyst, a process for preparing the same and use thereof The present catalyst comprises a cracking component and a hydrogenation component, wherein the cracking component comprises from 0 to 20 wt. % of a molecular sieve and from 20 wt. % to 60 wt. % of an amorphous silica-alumina, the hydrogenation component comprises at least one hydrogenation metal in a total amount of from 34 wt. % to 75 wt. % calculated by the mass of oxides, each amount is based on the total weight of the catalyst. The present catalyst is prepared by directly mixing an acidic component powder material with an impregnating solution, impregnating, filtering, drying, molding, and drying and calcining. 1. A process for preparing a hydrocracking catalyst , comprising the steps of(1) homogeneously mixing a precursor for an amorphous silica-alumina with an optional molecular sieve and an optional alumina;(2) formulating an impregnating solution comprising at least one hydrogenation metal;(3) impregnating the mixed powder in step (1) with the impregnating solution in step (2); and(4) filtering, drying, pulverizing, adding an adhesive or a peptizing agent, molding, drying, and calcining to obtain the hydrocracking catalyst.2. The process according to claim 1 , wherein the precursor for the amorphous silica-alumina is an amorphous gelatinous silica-alumina dry powder prepared by a method comprising(1) conducting a neutralization and gelatinization reaction of an acidic aluminum salt solution with a mixed solution of alkaline sodium silicate and sodium aluminate at a temperature ranging from 20° C. to 80° C. and a pH value ranging from 4.0 to 9.5;(2) adding at least one organosilicon source after gelatinization, wherein the at least one organosilicon source is chosen from organic silicon oils or silicon esters, the at least one organosilicon is added in an amount ranging from 5% to 40% relative to the total silicon amount present in the amorphous ...

CARBON-BASED, PRECIOUS METAL-TRANSITION METAL COMPOSITE CATALYST AND PREPARATION METHOD THEREFOR

The present invention relates to a carbon-based precious metal-transition metal composite catalyst and a preparation method therefor, and more particularly, to a catalyst synthesis method in which, when preparing a high-content precious metal-transition metal composite catalyst, a catalyst having uniform particles and composition can be prepared, and cyclohexane dimethanol (CHDM) is efficiently produced by the hydrogenation reaction of cyclohexane dicarboxylic acid (CHDA) in an aqueous solution. Provided is a method for preparing a carbon-based precious metal-transition metal composite catalyst, wherein, in the carbon-based precious metal-transition metal composite catalyst, the precious metal is included in an amount of 10-20 parts by weight, and the transition metal is included in an amount of 10-20 parts by weight based on 100 parts by weight of the composite catalyst, and thus a total amount of the precious metal-transition metal is 20-40 parts by weight based on 100 parts by weight of the composite catalyst.

AROMATIZATION OF LIGHT HYDROCARBONS USING METAL-DOPED ZEOLITE CATALYSTS WITH ENHANCED MESOPOROSITY

According to embodiments, a process for aromatizing hydrocarbons may include contacting the hydrocarbons with a zinc- or gallium-doped ZSM-5 catalyst having a mesopore volume of greater than 0.09 cm/g. Contacting the hydrocarbons with the catalyst causes a least a portion of the hydrocarbons to undergo chemical reactions to form aromatic hydrocarbons.

HYDROGENATION AND ETHYNYLATION CATALYSTS

A process for preparing a catalyst includes impregnating a metal oxide carrier with an aqueous solution to form an impregnated carrier; drying the impregnated carrier to form a dried, impregnated carrier; and heat-treating the dried, impregnated carrier in air to form the catalyst; wherein: the aqueous solution includes a copper salt; and from about 3 wt % to about 15 wt % of a C-Cmultifunctional carboxylic acid; and the catalyst includes from about 5 wt % to about 50 wt % copper oxide. 1. A process for forming a catalyst for hydrogenation , dehydrogenation , hydrogenolysis , or ethynylation , the process comprising:impregnating a metal oxide carrier with an aqueous solution to form an impregnated carrier;drying the impregnated carrier to form a dried, impregnated carrier; andheat-treating the dried, impregnated carrier to form the catalyst; [ a copper salt; and', {'sub': 3', '6, 'from about 1 wt % to about 15 wt % of a C-Cmultifunctional carboxylic acid; and'}], 'the aqueous solution comprises, 'the catalyst comprises from about 5 wt % to about 50 wt % copper oxide., 'wherein2. The process of claim 1 , wherein the copper salt comprises copper nitrate claim 1 , copper sulfate claim 1 , copper acetate claim 1 , copper chloride claim 1 , or copper citrate.3. The process of claim 1 , wherein the catalyst is an ethynylation catalyst and the aqueous solution further comprises a bismuth salt and the catalyst comprises up to about 5 wt % BiO.4. The process of claim 3 , wherein the bismuth salt comprises bismuth nitrate claim 3 , bismuth sulfate claim 3 , bismuth acetate claim 3 , bismuth chloride claim 3 , or bismuth citrate.5. The process of claim 1 , wherein the multifunctional carboxylic acid is a C-Cmulti-carboxylic acid.67-. (canceled)8. The process of claim 1 , wherein the catalyst is a hydrogenation claim 1 , dehydrogenation claim 1 , or hydrogenolysis catalyst and the aqueous solution consists essentially of the copper salt claim 1 , from about 1 wt % to about 15 ...

Hydrogenation and ethynylation catalysts

A process for preparing a catalyst includes impregnating a metal oxide carrier with an aqueous solution to form an impregnated carrier; drying the impregnated carrier to form a dried, impregnated carrier; and heat-treating the dried, impregnated carrier in air to form the catalyst; wherein: the aqueous solution includes a copper salt; and from about 3 wt % to about 15 wt % of a C3-C6 multifunctional carboxylic acid; and the catalyst includes from about 5 wt % to about 50 wt % copper oxide.

Hydrogen Oxidation Catalyst, Use Thereof, And Method For Hydrogen Recombination

A hydrogen oxidation catalyst is provided, comprising a zeolite that contains at least one catalytically active noble metal or a compound thereof, wherein said zeolite is a hydrophobic zeolite. A use of the catalyst and a method for hydrogen recombination in nuclear power plants, reprocessing plants or fuel element repositories is also specified.

Transition Metal-Catalyzed Production of Alcohol and Carbonyl Compounds From Hydrocarbons

Processes for converting a hydrocarbon reactant into an alcohol compound and/or a carbonyl compound are disclosed in which the hydrocarbon reactant and a supported transition metal catalyst—containing molybdenum, tungsten, or vanadium—are irradiated with a light beam at a wavelength in the UV-visible spectrum, optionally in an oxidizing atmosphere, to form a reduced transition metal catalyst, followed by hydrolyzing the reduced transition metal catalyst to form a reaction product containing the alcohol compound and/or the carbonyl compound. 1. A process for converting a hydrocarbon reactant into an alcohol compound and/or a carbonyl compound , the process comprising:(i) irradiating the hydrocarbon reactant and a supported transition metal catalyst comprising molybdenum, tungsten, vanadium, or a combination thereof, with a light beam at a wavelength in the UV-visible spectrum to reduce at least a portion of the supported transition metal catalyst to form a reduced transition metal catalyst; and(ii) hydrolyzing the reduced transition metal catalyst to form a reaction product comprising the alcohol compound and/or the carbonyl compound.2. The process of claim 1 , wherein step (i) comprises irradiating the hydrocarbon reactant and the supported transition metal catalyst in an oxidizing atmosphere.3. The process of claim 1 , wherein the hydrocarbon reactant comprises a Cto Clinear claim 1 , branched claim 1 , or cyclic alkane compound.4. The process of claim 1 , wherein the hydrocarbon reactant comprises a Cto Colefin compound claim 1 , a Cto Caromatic compound claim 1 , or any combination thereof.5. The process of claim 1 , wherein the supported transition metal catalyst contains from 0.01 to 50 wt. % of molybdenum claim 1 , tungsten claim 1 , vanadium claim 1 , or a combination thereof claim 1 , based on the weight of the supported transition metal catalyst.6. The process of claim 1 , wherein:the supported transition metal catalyst comprises a solid oxide, a chemically ...

Supported indium oxide catalyst and process for methanol synthesis using the same

The invention relates to a process for methanol synthesis comprising the steps of providing a syngas feed stream comprising hydrogen and carbon oxides selected from carbon dioxide or a mixture of carbon dioxide and carbon monoxide, wherein carbon dioxide represents from 1 to 50 mol % of the total molar content of the feed stream, carbon monoxide is contained from 0 to 85 mol % of the total molar content, and H2 is comprised from 5 to 95 mol % of the total molar content of the feed stream, and a catalyst comprising indium oxide (In2O3) on a support wherein the support comprises zirconium dioxide or is zirconium dioxide; putting in contact said stream with said supported catalyst at a reaction temperature of at least 373 K (99.85° C.) and under a pressure ranging of at least 1 MPa; and recovering the methanol effluents. The invention also relates to a supported indium oxide catalyst.

POROUS IRON-SILICATE WITH RADIALLY DEVELOPED BRANCH, AND IRON-CARBIDE/SILICA COMPOSITE CATALYST PREPARED THEREFROM

The present invention provides an iron-carbide/silica composite catalyst that is highly reactive to a Fischer-Tropsch synthesis by firstly forming an iron-silicate structure having large specific surface area and well-developed pores through a hydrothermal reaction of an iron salt with a silica particle having a nanostructure, and then activating the iron-silicate structure in a high temperature carbon monoxide atmosphere. When using the iron-carbide/silica composite catalyst according to the present invention in the Fischer-Tropsch synthesis reaction, it is possible to effectively prepare liquid hydrocarbon with a high CO conversion rate and selectivity. 1. A porous iron-silicate with radially developed branches formed by a hydrothermal reaction of an aqueous solution containing an iron salt hydrate and a silica particle whose a structure has a role as a transformation template.2. The porous iron-silicate of claim 1 , which is termed by a hydrothermal reaction of an aqueous solution containing a silica particle and an iron salt hydrate in basic conditions.3. The porous iron-silicate of claim 1 , wherein the silica particle has a regular-shaped nanostructure.4. A method of preparing a porous iron-silicate with radially developed branches claim 1 , comprising the steps of:(i) heating a silica solution wherein a silica particle is mixed with a basic reagent;(ii) introducing an aqueous solution containing an iron salt hydrate to said heated silica solution; and(iii) decomposing a mixed solution of the iron salt hydrate and silica through a high-temperature hydrothermal reaction to form the porous iron-silicate.5. The method of claim 4 , wherein the silica particle has a surface area of 50˜1000 m/g and a pore volume of 0.2˜cm/g.6. The method of claim 4 , wherein the basic reagent is sodium hydroxide and the amount of solid sodium hydroxide used is 0.5 to 2 times with respect to the weight of silica.7. The method of claim 4 , wherein the silica particle is a silica ...

METHOD FOR PRODUCING POROUS BODIES WITH ENHANCED PROPERTIES

A precursor mixture for producing a porous body, wherein the precursor mixture comprises: (i) milled alpha alumina powder having a particle size of 0.1 to 6 microns, (ii) boehmite powder that functions as a binder of the alpha alumina powders, and (iii) burnout materials having a particle sizes of 1-10 microns. In some embodiments, an unmilled alpha alumina powder having a particle size of 10 to 100 microns is also included in said precursor mixture. Also described herein is a method for producing a porous body in which the above-described precursor mixture is formed to a given shape, and subjected to a heat treatment step in which the formed shape is sintered to produce the porous body. 1. A method for producing a porous body , the method comprising:providing a precursor mixture comprising (i) milled alpha alumina powder having a particle size of 0.1 to 6 microns, (ii) boehmite powder that functions as a binder of the alpha alumina powders, and (iii) burnout material having a particle size of 1-10 microns;forming a predetermined shape; andsubjecting the shape to a heat treatment step in which the shape is sintered to produce the porous body.2. The method of claim 1 , further comprising unmilled alpha alumina powder having a particle size of 10 to 100 microns in said precursor mixture.3. The method of claim 2 , wherein the weight ratio of milled to unmilled alpha alumina powder is in a range of 0.25:1 to about 5:1.4. The method of claim 1 , wherein unmilled alpha alumina powder is excluded from the precursor mixture.5. The method of claim 1 , wherein the method comprises:(i) dispersing boehmite into water to produce a dispersion of boehmite;(ii) adding a milled alpha alumina powder having a particle size of 0.1 to 6 microns to the dispersion of boehmite, and mixing until a first homogeneous mixture is obtained, wherein said boehmite functions as a binder of the alpha alumina powder;(iii) adding burnout materials having a particle size of 1-10 microns, and mixing ...

FISCHER-TROPSCH PROCESS IN THE PRESENCE OF A CATALYST PREPARED FROM A MOLTEN SALT

Fischer-Tropsch process for the synthesis of hydrocarbons by bringing a feedstock including synthesis gas into contact with a catalyst prepared by the following: 1. Fischer-Tropsch process for the synthesis of hydrocarbons , which comprises bringing a feedstock comprising a synthesis gas into contact with at least one catalyst under a total pressure between 0.1 and 15 MPa , at a temperature of between 150 and 350° C. , and at an hour space velocity of between 100 and 20 000 volumes of synthesis gas per volume of catalyst and per hour with an H/CO molar ratio of the synthesis gas between 0.5 and 4 , said catalyst containing an active phase comprising at least cobalt and a porous support of oxide type , said catalyst being prepared by at least the following steps:a) said porous oxide-type support is brought into contact with a cobalt metal salt of which the melting point of said cobalt metal salt is between 30 and 150° C., in order to form a solid mixture for a period of time of between 5 minutes and 5 hours, the weight ratio of said cobalt metal salt to said porous oxide support being between 0.1 and 1;b) the solid mixture obtained at the end of step a) is heated with stirring under atmospheric pressure at a temperature between the melting point of said cobalt metal salt and 200° C. for a period of time of between 5 minutes and 12 hours;c) optionally, the solid obtained at the end of step b) is dried at a temperature below 200° C.;d) the solid obtained at the end of step b) or c) is calcined at a temperature above 200° C. and below or equal to 1100° C. under an inert atmosphere or under an oxygen-containing atmosphere.2. Process according to claim 1 , in which said cobalt metal salt is chosen from cobalt nitrate hexahydrate or cobalt acetate tetrahydrate.3. Process according to claim 1 , in which the weight ratio of the cobalt metal salt to the porous support is between 0.3 and 0.9.4. Process according to claim 1 , in which step a) is carried out for 10 minutes to 4 ...

PROCESS FOR PREPARING A CATALYST OR A TRAPPING MASS FROM MOLTEN SALTS

Process for preparing a catalyst or a trapping mass comprising the following steps: 1. Process for preparing a catalyst or a trapping mass comprising an active phase based on at least one metal from group VIB , VIIB , VIIIB , IB or MB and a porous oxide support , said catalyst being prepared by at least the following steps:a) said porous oxide support is brought into contact with at least one metal salt comprising at least one metal belonging to groups VIB, VIIB, VIIIB, IB or IIB, of which the melting point of said metal salt is between 20° C. and 150° C., for a period of between 5 minutes and 5 hours in order to form a solid mixture, the weight ratio of said metal salt to said porous oxide support being between 0.1 and 1;b) the solid mixture obtained at the end of step a) is heated with stirring at a temperature between the melting point of said metal salt and 200° C. and with a residence time of between 5 minutes and 12 hours;c) optionally, the solid obtained at the end of step b) is dried at a temperature below 200° C.;d) the solid obtained at the end of step b) or c) is calcined at a temperature above 200° C. and below or equal to 1100° C. under an inert atmosphere or under an oxygen-containing atmosphere.2. Process according to claim 1 , in which said metal is chosen from Zn claim 1 , Cu claim 1 , Ni claim 1 , Fe claim 1 , Co claim 1 , Mn.3. Process according to claim 1 , in which the metal salt is a hydrated nitrate salt.4. Process according to claim 3 , in which said metal salt is chosen from zinc nitrate trihydrate claim 3 , zinc nitrate hexahydrate claim 3 , copper nitrate trihydrate claim 3 , copper nitrate hexahydrate claim 3 , nickel nitrate hexahydrate claim 3 , iron nitrate nonahydrate claim 3 , cobalt nitrate hexahydrate claim 3 , manganese nitrate tetrahydrate claim 3 , manganese nitrate hexahydrate claim 3 , taken alone or as a mixture.5. Process according to claim 1 , in which the weight ratio of said metal salt to the porous support is between 0.3 ...

METHOD FOR ADDING AN ORGANIC COMPOUND TO A POROUS SOLID IN THE GASEOUS PHASE

The invention relates to a process for adding an organic compound to a porous solid wherein the porous solid and the organic compound in the liquid state are brought together simultaneously, without physical contact between the solid and the organic compound in the liquid state, at a temperature below the boiling point of the organic compound and under pressure and time conditions such that a fraction of said organic compound is transferred gaseously to the porous solid. 1) A process for adding an organic compound to a porous solid comprising a step a) wherein the porous solid and the organic compound in the liquid state are brought together simultaneously and without physical contact between the solid and the organic compound in the liquid state , at a temperature below the boiling point of the organic compound and under pressure and time conditions such that a fraction of said organic compound is transferred gaseously to the porous solid.2) The process as claimed in claim 1 , wherein step a) is carried out by means of a unit for adding said organic compound comprising a first compartment and a second compartment that are in communication so as to allow the passage of a gaseous fluid between the compartments claim 1 , the first compartment containing the porous solid and the second compartment containing the organic compound in the liquid state.3) The process as claimed in claim 2 , wherein the unit comprises a chamber that includes the first and second compartments claim 2 , the two compartments being in gaseous communication.4) The process as claimed in claim 2 , wherein the unit comprises two chambers that respectively form the first and second compartments claim 2 , the two chambers being in gaseous communication.5) The process as claimed in claim 1 , wherein step a) of bringing the porous solid together with the organic compound in the liquid state is carried out in the presence of a stream of a carrier gas flowing from the second compartment into the first ...

Methods of Preparing a Catalyst

A method comprising a) drying a support material comprising silica at temperature in the range of from about 150° C. to about 220° C. to form a dried support; b) contacting the dried support with methanol to form a slurried support; c) subsequent to b), cooling the slurried support to a temperature of less than about 60° C. to form a cooled slurried support; d) subsequent to c), contacting the cooled slurried support with a titanium alkoxide to form a titanated support; and e) thermally treating the titanated support by heating to a temperature of equal to or greater than about 150° C. for a time period of from about 5 hours to about 30 hours to remove the methanol and yield a dried titanated support. 1. A method comprising:a) drying a support material comprising silica at temperature in the range of from about 150° C. to about 220° C. to form a dried support;b) contacting the dried support with methanol to form a slurried support;c) subsequent to b), cooling the slurried support to a temperature of less than about 60° C. to form a cooled slurried support;d) subsequent to c), contacting the cooled slurried support with a titanium alkoxide to form a titanated support; ande) thermally treating the titanated support by heating to a temperature of equal to or greater than about 150° C. for a time period of from about 5 hours to about 30 hours to remove the methanol and yield a dried titanated support.2. The method of further comprising the addition of a chromium-containing compound prior to the complete removal of methanol to form a precatalyst.3. The method of further comprising the addition of water in an amount ranging from about 0.1 to about 10 moles per mole of titanium after addition of the titanium alkoxide.4. The method of further comprising calcining the precatalyst at a temperature in the range of from about 400° C. to about 1000° C. for a time period of from about 30 minutes to about 24 hours to form a polymerization catalyst.5. The method of wherein the ...

Mesoporous Carbon Modified with Polyethylenimine Catalysis Bisphenol A in Organic Solvent

An enzyme immobilized on a porous structure can oxidize phenol compounds. 1. A composite comprising:a porous carbon carrier;a polymer coating on a surface of the porous carbon carrier; andan enzyme associated with the polymer.2. The composite of claim 1 , wherein the porous carbon carrier includes carbon nanoparticles claim 1 , carbon black or a mesoporous carbon.3. The composite of claim 1 , wherein the porous carbon carrier includes a mesoporous carbon.4. The composite of claim 1 , wherein the porous carbon carrier has a pore-size distribution of about 10 to 50 nm claim 1 , 15 to 50 nm or 20 to 25 nm.5. The composite of claim 1 , wherein the porous carbon carrier has a pore-size distribution of about 15 to 50 nm.6. The composite of claim 1 , wherein the porous carbon carrier has a pore-size distribution of about 20 to 25 nm.7. The composite of claim 1 , wherein the porous carbon carrier has a specific surface area of between 300 and 800 mg.8. The composite of claim 1 , wherein the porous carbon carrier has a pore volume of between 1.5 and 2.5 cmg.9. The composite of claim 1 , wherein the polymer includes a plurality of amino groups.10. The composite of claim 1 , wherein the polymer includes polyethyleneimine claim 1 , a polyethylene glycol claim 1 , a polyacrylate claim 1 , triethylaminoethyl cellulose claim 1 , diethylaminoethyl cellulose claim 1 , cellulose claim 1 , carboxymethyl cellulose claim 1 , bovine serum albumin (BSA) claim 1 , or a lysozyme.11. The composite of claim 1 , wherein the polymer includes polyethyleneimine or a triethylaminoethyl cellulose.12. The composite of claim 1 , wherein the enzyme is a tyrosinase.13. A method of oxidizing a phenol comprising:suspending a composite including a porous carbon carrier, a polymer coating on a surface of the porous carbon carrier, and an enzyme associated with the polymer in an organic solvent; andexposing the composite to a phenol in the organic solvent.14. The method of claim 13 , wherein the enzyme is a ...

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

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

HYDROISOMERIZATION CATALYST WITH A BASE EXTRUDATE HAVING A HIGH NANOPORE VOLUME

The present invention is directed to an improved finished hydroisomerization catalyst manufactured from a first high nanopore volume (HNPV) alumina having a broad pore size distribution (BPSD), and a second HNPV alumina having narrow pore size distribution (NPSD). Their combination yields a HNPV base extrudate having larger porosity with a bimodal pore size distribution as compared to a conventional base extrudates. 1. A hydroisomerization catalyst , comprising:a base extrudate comprising at least one molecular sieve selective towards isomerization of n-paraffins, a first alumina having a high nanopore volume and a broad pore size distribution, and a second alumina having a high nanopore volume and a narrow pore size distribution, wherein the base extrudate has a nanopore volume in the 6 nm to 11 nm range of 0.25 to 0.4 cc/g; andat least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table.2. The hydroisomerization catalyst of claim 1 , wherein the first alumina has a pore size distribution characterized by a full width at half-maximum claim 1 , normalized to pore volume claim 1 , of 15 to 25 nm·g/cc.3. The hydroisomerization catalyst of claim 2 , wherein the first alumina has a nanopore volume in the 2 nm to 50 nm range of 0.7 to 2 cc/g4. The hydroisomerization catalyst of claim 2 , wherein the second alumina has a pore size distribution characterized by a full width at half-maximum claim 2 , normalized to pore volume claim 2 , of 5 to 15 nm·g/cc.5. The hydroisomerization catalyst of claim 4 , wherein the second alumina has a nanopore volume in the 2 nm to 50 nm range of 0.7 to 2 cc/g.6. The hydroisomerization catalyst of claim 1 , wherein a pore size distribution plot for the base extrudate will indicate a maximum peak with a shoulder located at a pore size between 7 and 14 nm.7. The hydroisomerization catalyst of claim 1 , wherein the base extrudate has a nanopore volume in the 6 nm to 11 nm range of ...

HYDROISOMERIZATION CATALYST WITH A BASE EXTRUDATE HAVING A HIGH TOTAL NANOPORE VOLUME

The present invention is directed to an improved finished hydroisomerization catalyst manufactured from a first high nanopore volume (HNPV) alumina having a broad pore size distribution (BPSD), and a second HNPV alumina having narrow pore size distribution (NPSD). Their combination yields a HNPV base extrudate having higher total nanopore volume with a bimodal pore size distribution as compared to a conventional base extrudates. 1. A hydroisomerization catalyst , comprising:a base extrudate comprising at least one molecular sieve selective towards isomerization of n-paraffins, a first alumina having a high nanopore volume and a broad pore size distribution, and a second alumina having a high nanopore volume and a narrow pore size distribution, wherein the base extrudate has a total nanopore volume in the 2 nm to 50 nm range of 0.7 to 1.2 cc/g; andat least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table.2. The hydroisomerization catalyst of claim 1 , wherein the first alumina has a pore size distribution characterized by a full width at half-maximum claim 1 , normalized to pore volume claim 1 , of 15 to 25 nm·g/cc.3. The hydroisomerization catalyst of claim 2 , wherein the first alumina has a nanopore volume in the 2 nm to 50 nm range of 0.7 to 2 cc/g4. The hydroisomerization catalyst of claim 2 , wherein the second alumina has a pore size distribution characterized by a full width at half-maximum claim 2 , normalized to pore volume claim 2 , of 5 to 15 nm·g/cc.5. The hydroisomerization catalyst of claim 4 , wherein the second alumina has a nanopore volume in the 2 nm to 50 nm range of 0.7 to 2 cc/g.6. The hydroisomerization catalyst of claim 1 , wherein a pore size distribution plot for the base extrudate will indicate a maximum peak with a shoulder located at a pore size between 7 and 14 nm.7. The hydroisomerization catalyst of claim 1 , wherein the base extrudate has a nanopore volume in the 6 nm ...

HYDROISOMERIZATION CATALYST WITH A BASE EXTRUDATE HAVING A LOW PARTICLE DENSITY

The present invention is directed to an improved finished hydroisomerization catalyst manufactured from a first high nanopore volume (HNPV) alumina having a broad pore size distribution (BPSD), and a second HNPV alumina having narrow pore size distribution (NPSD). Their combination yields a HNPV base extrudate having a low particle density as compared to a conventional base extrudates. 1. A hydroisomerization catalyst , comprising:a base extrudate comprising at least one molecular sieve selective towards isomerization of n-paraffins, a first alumina having a high nanopore volume and a broad pore size distribution, and a second alumina having a high nanopore volume and a narrow pore size distribution, wherein the base extrudate has a particle density of 0.75 to 0.95 cc/g; andat least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table.2. The hydroisomerization catalyst of claim 1 , wherein the first alumina has a pore size distribution characterized by a full width at half-maximum claim 1 , normalized to pore volume claim 1 , of 15 to 25 nm·g/cc.3. The hydroisomerization catalyst of claim 2 , wherein the first alumina has a nanopore volume in the 2 nm to 50 nm range of 0.7 to 2 cc/g4. The hydroisomerization catalyst of claim 2 , wherein the second alumina has a pore size distribution characterized by a full width at half-maximum claim 2 , normalized to pore volume claim 2 , of 5 to 15 nm·g/cc.5. The hydroisomerization catalyst of claim 4 , wherein the second alumina has a nanopore volume in the 2 nm to 50 nm range of 0.7 to 2 cc/g.6. The hydroisomerization catalyst of claim 1 , wherein a pore size distribution plot for the base extrudate will indicate a maximum peak with a shoulder located at a pore size between 7 and 14 nm.7. The hydroisomerization catalyst of claim 1 , wherein the base extrudate has a nanopore volume in the 6 nm to 11 nm range of 0.25 to 0.4 cc/g claim 1 , a nanopore volume in the 11 ...

HYDROISOMERIZATION CATALYST MANUFACTURED USING A HIGH NANOPORE VOLUME ALUMINA SUPPORTS

The present invention is directed to an improved finished hydroisomerization catalyst manufactured from a first high nanopore volume (HNPV) alumina and a pore size distribution characterized by a full width at half-maximum, normalized to pore volume, of 15 to 25 nm·g/cc, and a second HNPV alumina having a pore size distribution characterized by a full width at half-maximum, normalized to pore volume, of 5 to 15 nm·g/cc. Their combination yields a HNPV base extrudate having a low particle density as compared to a conventional base extrudates. 1. A hydroisomerization catalyst , comprising: at least one molecular sieve selective towards isomerization of n-paraffins,', 'a first alumina having a high nanopore volume and a pore size distribution characterized by a full width at half-maximum, normalized to pore volume, of 15 to 25 nm·g/cc, and', 'a second alumina having a high nanopore volume and a pore size distribution characterized by a full width at half-maximum, normalized to pore volume, of 5 to 15 nm·g/cc;, 'a base extrudate comprising'}the catalyst further comprising at least one metal selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table.2. The hydroisomerization catalyst of claim 1 , wherein the first alumina has a nanopore volume in the 2 nm to 50 nm range of 0.7 to 2 cc/g3. The hydroisomerization catalyst of claim 2 , wherein the second alumina has a nanopore volume in the 2 nm to 50 nm range of 0.7 to 2 cc/g.4. The hydroisomerization catalyst of claim 1 , wherein the second alumina has a nanopore volume in the 2 nm to 50 nm range of 0.7 to 2 cc/g.5. The hydroisomerization catalyst of claim 1 , wherein a pore size distribution plot for the base extrudate will indicate a maximum peak with a shoulder located at a pore size between 7 and 14 nm.6. The hydroisomerization catalyst of claim 1 , wherein the base extrudate has a nanopore volume in the 6 nm to 11 nm range of 0.25 to 0.4 cc/g claim 1 , a nanopore volume ...

Hydrotreating Catalyst for Heavy Hydrocarbon Oil, Method for Producing the Same, and Method for Hydrotreating Heavy Hydrocarbon Oil

Provided is a hydrotreating catalyst for a heavy hydrocarbon oil, the catalyst including an inorganic oxide carrier including alumina as a main component and a metal component supported on the inorganic oxide carrier, the catalyst having a specific surface area within a predetermined range, a reduction peak temperature that is lower than 450° C. in temperature-programmed reduction measurement of the catalyst and that is higher than or equal to a predetermined temperature, and an amount of nitrogen monoxide adsorbed on the sulfided catalyst within a predetermined range.

Catalyst

A catalyst for producing unsaturated aldehyde and unsaturated carboxylic acid, wherein the cumulative pore volume (A) of pores having a pore diameter of 1 μm or more and 100 μm or less, in the catalyst, is 0.12 ml/g or more and 0.19 ml/g or less, and the ratio (A/B) of the cumulative pore volume (A) to the cumulative pore volume (B) of pores having a pore diameter of 1 μm or more and 100 μm or less, in a pulverized product not passing through a Tyler 6 mesh, in a pulverized product obtained by pulverization of the catalyst under a particular condition is 0.30 or more and 0.87 or less.

HIGH NANOPORE VOLUME CATALYST AND PROCESS USING SSZ-91

An improved hydroisomerization catalyst and process for making a base oil product wherein the catalyst comprises a base extrudate that includes SSZ-91 molecular sieve and a high nanopore volume alumina. The catalyst and process generally involves the use of a SSZ-91/high nanopore volume alumina based catalyst to produce dewaxed base oil products by contacting the catalyst with a hydrocarbon feedstock. The catalyst base extrudate advantageously comprises an alumina having a pore volume in the 11-20 nm pore diameter range of 0.05 to 1.0 cc/g, with the base extrudate formed from SSZ-91 and the alumina having a total pore volume in the 2-50 nm pore diameter range of 0.12 to 1.80 cc/g. The catalyst and process provide improved base oil yield with reduced gas and fuels production. 1. A hydroisomerization catalyst , useful to make dewaxed products including base oils , comprisinga base extrudate comprising an SSZ-91 molecular sieve and an alumina, wherein the alumina has a pore volume in the 11-20 nm pore diameter range of 0.05 to 1.0 cc/g and the base extrudate has a total pore volume in the 2-50 nm pore diameter range of 0.12 to 1.80 cc/g; andat least one modifier selected from Groups 6 to 10 and Group 14 of the Periodic Table.2. The catalyst of claim 1 , wherein the modifier comprises a Group 8-10 metal of the Periodic Table.3. The catalyst of claim 2 , wherein the modifier is a Group 10 metal comprising Pt.4. The catalyst of claim 1 , wherein the alumina has a pore volume in the 6-11 nm pore diameter range of 0.05 to 1.0 cc/g claim 1 , or a pore volume in the 6-11 nm pore diameter range of 0.06 to 0.8 cc/g claim 1 , or a pore volume in the 6-11 nm pore diameter range of 0.07 to 0.6 cc/g.5. The catalyst of claim 1 , wherein the alumina has a pore volume in the 11-20 nm pore diameter range of 0.07 to 0.85 cc/g claim 1 , or a pore volume in the 11-20 nm pore diameter range of 0.09 to 0.7 cc/g.6. The catalyst of claim 1 , wherein the alumina has a pore volume in the 20-50 ...

POROUS MONOLITH CONTAINING TiO2 AND METHOD FOR THE PRODUCTION THEREOF

The invention relates to a porous monolith comprising between 20 wt.-% and 70 wt.-% Ti0 2 relative to the total weight of the monolith, and between 30 wt.-% and 80 wt.-% a refractory oxide, selected from silica, alumina or silica-alumina, relative to the total weight of the monolith, characterized in that said porous monolith has a bulk density of less than 0.19 g/mL. 1. A porous monolith comprising between 20% and 70% by weight of TiOrelative to the total weight of the monolith , between 30% and 80% by weight of a refractory oxide selected from silica , alumina or silica-alumina relative to the total weight of the monolith , characterized in that said porous monolith comprises a bulk density of less than 0.19 g/ml.2. The monolith as claimed in claim 1 , characterized in that said porous monolith comprises a bulk density of less than 0.16 g/ml.3. The monolith as claimed in claim 1 , characterized in that it comprises a mesoporous volume of from 0.1 to 1 ml/g for a pore diameter between 0.2 and 50 nm.4. The monolith as claimed in claim 1 , characterized in that it comprises a type-I macroporous volume claim 1 , of which the pore diameter is greater than 50 nm and less than or equal to 1000 nm claim 1 , of between 0.1 and 3 ml/g.5. The monolith as claimed in claim 1 , characterized in that it comprises a type-II macroporous volume claim 1 , of which the pore diameter is greater than 1 μm and less than or equal to 10 μm claim 1 , of between 0.1 and 8 ml/g.6. The monolith as claimed in claim 1 , characterized in that it comprises a mesoporosity and/or a type-I macroporosity and/or a type-II macroporosity.7. The monolith as claimed in claim 1 , characterized in that it also comprises a macroporous volume of less than 0.5 ml/g for a pore diameter of greater than 10 μm.8. The monolith as claimed in claim 1 , characterized in that it comprises a BET specific surface area of between 150 and 700 m/g.9. The monolith as claimed in claim 1 , characterized in that it also ...

METHOD FOR FORMING CARBON-CARBON BOND

A method for forming a carbon-carbon bond, wherein a reaction is performed by filling a platinum group metal-supported catalyst into a filling container, and passing a raw material liquid through the platinum group metal-supported catalyst in a continuous circulation manner, and wherein the platinum group metal-supported catalyst is a platinum group metal-supported catalyst in which nanoparticles of a platinum group metal with an average particle diameter of 1 to 100 nm are supported on a non-particulate organic porous ion exchanger formed of a continuous framework phase and a continuous pore phase. 1. A method for forming a carbon-carbon bond to form a carbon-carbon bond by performing (1) reaction of an aromatic halide with an organoboron compound , (2) reaction of an aromatic halide with a compound having a terminal alkynyl group , or (3) a reaction of an aromatic halide with a compound having an alkenyl group ,wherein the carbon-carbon bond-forming reaction is performed by introducing a raw material liquid (i) containing the aromatic halide and the organoboron compound, a raw material liquid (ii) containing the aromatic halide and the compound having a terminal alkynyl group, or a raw material liquid (iii) containing the aromatic halide and the compound having an alkenyl group, through an introduction path of a filling container filled with a platinum group metal-supported catalyst, into the filling container, passing the raw material liquid through the platinum group metal-supported catalyst, and discharging the reaction liquid from a discharge path of the filling container, andwherein the platinum group metal-supported catalyst is a platinum group metal-supported catalyst in which nanoparticles of a platinum group metal with an average particle diameter of 1 to 100 nm are supported on a non-particulate organic porous ion exchanger, and the non-particulate organic porous ion exchanger is formed of a continuous framework phase and a continuous pore phase; has a ...

CARBIDE-DERIVED CARBONS HAVING INCORPORATED METAL CHLORIDE OR METALLIC NANOPARTICLES

Carbide-derived carbons are provided that have high dynamic loading capacity for high vapor pressure gasses such as HS, SO, or NH. The carbide-derived carbons can have a plurality of metal chloride or metallic nanoparticles entrapped therein. Carbide-derived carbons are provided by extracting a metal from a metal carbide by chlorination of the metal carbide to produce a porous carbon framework having residual metal chloride nanoparticles incorporated therein, and annealing the porous carbon framework with Hto remove residual chloride by reducing the metal chloride nanoparticles to produce the metallic nanoparticles entrapped within the porous carbon framework. The metals can include Fe, Co, Mo, or a combination thereof. The carbide-derived carbons are provided with an ammonia dynamic loading capacity of 6.9 mmol gto 10 mmol gat a relative humidity of 0% RH to 75% RH. 1. A carbide-derived carbon comprising a plurality of metal nanoparticles entrapped therein , the carbide derived carbon made by the steps of:extracting a metal from a metal carbide by chlorination of the metal carbide at a temperature of 500° C. to 700° C. for a period of time from 0.25 hours to 2 hours to produce a porous carbon framework having residual metal chloride nanoparticles incorporated therein, and{'sub': '2', 'annealing the porous carbon framework with Hto remove residual chloride by reducing the metal chloride nanoparticles to produce the metallic nanoparticles entrapped within the porous carbon framework,'}wherein the metal is selected from the group consisting of Fe, Mo, and a combination thereof,{'sup': 2', '−1', '2', '−1, 'wherein the carbide-derived carbon has a surface area of 300 mgto 900 mg, and'}{'sup': −1', '−1, 'wherein the carbide-derived carbon has a pore volume of 0.25 cc gto 0.5 cc g.'}2. A carbide-derived carbon comprising a porous carbon framework having a plurality of metal chloride or metallic nanoparticles entrapped therein ,wherein the nanoparticles comprise a metal ...

PREPARATION OF CATALYST

A process for preparing a hydrocarbon conversion catalyst that comprises a specially made silica-alumina composition and a metal or metal compound selected from Group VIB and Group VIII metals. The silica-alumina composition is made by preparing an aqueous mixture containing aluminum sulfate followed by adding alkali metal aluminate to the mixture to enhance the pH to within specified range and then adding aluminum sulfate to the mixture to lower the pH. Then alkali metal silicate is added followed by several other pH swings to provide a mixture containing silica-alumina. The resulting mixture is treated with an alkaline solution to provide a precipitate solid that is recovered to obtain a silica-alumina composition containing of from 30 to 70% wt silica and of from 70 to 30% wt of alumina. 1. A process for hydrocracking a hydrocarbonaceous feedstock , which process comprises: contacting a gaseous feedstock at a reaction temperature in the range of 250 to 500° C. and a total pressure at the reactor inlet in the range of from 3×10to 3×10Pa in the presence of hydrogen with a hydroconversion catalyst in which the gaseous feedstock contains less than 150 parts per million by weight of ammonia;wherein said hydroconversion catalyst is made by the method comprising;(a) preparing an aqueous mixture containing aluminum sulfate and having a pH in the range of from 1.0 to 6.5;(b) adding alkali metal aluminate to the mixture obtained in step (a) to increase the pH of the mixture to within the range of from 7.1 to 12;(c) adding aluminum sulfate to the mixture obtained in step (b) to lower the pH of the mixture to within the range of from 1.5 to 6.5;(d) adding alkali metal silicate to the mixture obtained in step (c) to increase the pH of the mixture to within the range of from 6.5 to 11,wherein the final steps of the preparation process are(v) adding aluminum sulfate to the mixture obtained in a process comprising steps (a)-(d) to lower the pH of the mixture to within the range ...

ACTIVE PHASE BIMODAL COMMIXED CATALYST, PROCESS FOR ITS PREPARATION AND USE IN HYDROTREATING RESIDUE

A hydroconversion catalyst with a bimodal pore structure: 1. Procedure for preparing an active phase commixing catalyst , comprising at least one metal from the periodic table group VI B , possibly at least one metal from group VIII of the periodic table , possibly phosphorus and a predominantly aluminium calcined matrix oxide , comprising the following steps:a) a step dissolving in water an acid aluminium precursor chosen from among aluminium sulphate, aluminium chloride and aluminium nitrate at a temperature between 20 and 90° C., a pH between 0.5 and 5, for a period between 2 and 60 minutes;b) a step for adjusting the pH by adding into the suspension obtained in step a) at least one base precursor chosen from among sodium aluminate, potassium aluminate, ammonia, sodium hydroxide, or potassium hydroxide, at a temperature between 20 and 90° C., with a pH between 7 and 10, between 5 and 30 minutes.(c) a step for co-precipitation of the suspension obtained after step b) by adding into the suspension at least one base precursor chosen between sodium aluminate, potassium aluminate, ammonia, sodium hydroxide or potassium hydroxide and at least one acid precursor selected from aluminium sulphate, aluminium chloride, aluminium nitrate, sulphuric acid, hydrochloric acid or nitric acid, at least one base or acid precursor comprising aluminium; the relative flow rate of the acidic and base precursors is chosen so as to obtain a pH of the reaction medium between 7 and 10 and the flow rate of the acidic and base precursors comprising aluminium is set so as to obtain a final alumina concentration in the suspension of between 10 and 38 g/l;d) a step for filtering the suspension obtained after step c) co-precipitation to obtain alumina gel;e) a step for drying the alumina gel obtained in step d) to obtain a powder;f) a step for heat treating the powder resulting from step e) at a temperature between 500 and 1000° C., for between 2 and 10 hrs in the presence or not of an air flow ...

SUPPORTED CATALYST, PREPARATION METHOD THEREFOR AND APPLICATION THEREOF

A supported catalyst has a support and a metal active component disposed on the support. The metal active component is at least one selected from the group consisting of a Group VIB metal element and a Group VIII metal element. The support contains at least one of heat-resistant inorganic oxides and molecular sieves and includes an internal channel penetrating the support. The ratio of the cross-section area of the channel to the cross-section area of the support is 0.05-3:100. The difference R between the water absorption rate and the BET pore volume of the support is not less than 0.2 mL/g. The supported catalyst can be used as a hydrogenation catalyst. When used in the hydrocracking of hydrocarbon oils, it can achieve high catalytic activity and high yield of jet fuels at the same time. The supported catalyst can also be used as a Fischer-Tropsch synthesis catalyst. 1. A supported catalyst , comprising a support and a metal active component supported on the support ,wherein the metal active component is at least one selected from the group consisting of a Group VIB metal element and a Group VIII metal element;wherein the support contains at least one of heat-resistant inorganic oxides and molecular sieves;wherein the support includes an internal channel penetrating the support, wherein the ratio of the cross-section area of the channel to the cross-section area of the support is 0.05-3:100; andwherein the difference R between the water absorption rate and the BET pore volume of the support is not less than 0.2 mL/g.2. The catalyst of claim 1 , wherein the Group VIB metal element is Mo and/or W claim 1 , and the Group VIII metal element is Co and/or N claim 1 , andwherein, based on the total amount of the catalyst, the Group VIB metal element is present in an amount of 10-35 wt %; the Group VIII metal element is present in an amount of 2-15 wt %; and the support is present in an amount of 50-88 wt %, all on oxide basis.3. The catalyst of claim 1 , wherein the heat ...

MESOPOROUS AND MACROPOROUS CATALYST FOR HYDROCONVERSION OF RESIDUES AND PREPARATION METHOD

Process of preparing hydroconversion catalyst comprising: 2. Process according to claim 1 , wherein the alumina concentration of the suspension of alumina gel obtained in stage c) is comprised between 13 and 35 g/l.3. Process according to claim 2 , wherein the alumina concentration of the suspension of alumina gel obtained in stage c) is comprised between 15 and 33 g/l.4. Process according to claim 1 , wherein the acidic precursor is aluminium sulphate.5. Process according to claim 1 , wherein the basic precursor is sodium aluminate.6. Process according to in which claim 1 , in stages a) claim 1 , b) claim 1 , c) claim 1 , the aqueous reaction medium is water and said stages are carried out with stirring claim 1 , in the absence of organic additive.7. Process according to claim 1 , wherein the acidic precursor of stage a) is introduced in a quantity corresponding to 0.5 to 4% by weight of the total alumina formed at the end of stage c).8. Mesoporous and macroporous hydroconversion catalyst prepared by the process according to .9. Mesoporous and macroporous hydroconversion catalyst according to having:{'sup': '2', 'a specific surface area Sbet greater than 110 m/g,'}a median mesopore diameter by volume comprised between 18 nm and 26 nm,a median macropore diameter by volume comprised between 100 and 1200 nm inclusive,a mesopore volume as measured with a mercury intrusion porosimeter greater than or equal to 0.70 ml/ga total pore volume measured by mercury porosimetry greater than or equal to 0.85 ml/g,a macropore volume comprised between 17 and 35% of the total pore volume,absence of micropores.10. Mesoporous and macroporous hydroconversion catalyst according to claim 9 , having a macropore volume comprised between 20 and 30% of the total pore volume.11. Mesoporous and macroporous hydroconversion catalyst according to claim 8 , having a median mesopore diameter by volume determined with a mercury intrusion porosimeter comprised between 19 and 25 nm and a median ...

Methods of Preparing a Catalyst Utilizing Hydrated Reagents

A pre-catalyst composition comprising a) a silica support comprising silica wherein an amount of silica ranges from about 70 wt. % to about 95 wt. % based upon a total weight of the silica support, b) a chromium-containing compound wherein an amount of chromium ranges from about 0.1 wt. % to about 5 wt. % based upon the amount of silica, c) a titanium-containing compound wherein an amount of titanium ranges from about 0.1 wt. % to about 20 wt. % based upon the amount of silica, d) a carboxylic acid wherein an equivalent molar ratio of titanium-containing compound to carboxylic acid ranges from about 1:1 to about 1:10, and e) a nitrogen-containing compound with a molecular formula containing at least one nitrogen atom wherein an equivalent molar ratio of titanium-containing compound to nitrogen-containing compound ranges from about 1:0.5 to about 1:10. 1. A method comprising:a) contacting a solvent and a carboxylic acid to form an acidic mixture wherein a weight ratio of solvent to carboxylic acid in the acidic mixture is from about 1:1 to about 100:1;b) contacting a titanium-containing compound and the acidic mixture to form an acidic titanium mixture wherein an equivalent molar ratio of titanium-containing compound to carboxylic acid in the acidic titanium mixture is from about 1:1 to about 1:4;c) contacting a nitrogen-containing compound and the acidic titanium mixture to form a solubilized titanium mixture wherein an equivalent molar ratio of titanium-containing compound to nitrogen-containing compound in the solubilized titanium mixture is from about 1:1 to about 1:4 and a pH of the solubilized titanium mixture is less than about 5.5; andd) contacting a chromium-silica support comprising from about 0.1 wt. % to about 20 wt. % water and the solubilized titanium mixture to form an addition product and drying the addition product by heating to a temperature in a range of from about 50° C. to about 150° C. and maintaining the temperature in the range of from about ...

CATALYSTS SYSTEMS THAT INCLUDE METAL CO-CATALYSTS FOR THE PRODUCTION OF PROPYLENE

Embodiments of methods of synthesizing a metathesis catalyst system, which include impregnating tungsten oxide on silica support in the presence of a precursor to produce a base catalyst; calcining the base catalyst; dispersing a solid metal-based co-catalyst onto the surface of the base catalyst to produce a doped catalyst; and calcining the doped catalyst to produce a metathesis catalyst system. Further embodiments of processes for the production of propylene, which include contacting a hydrocarbon feedstock comprising a mixture of 1-butene and 2-butene with embodiments of the metathesis catalyst system to produce, via metathesis conversion, a product stream comprising propylene. 1. A method of synthesizing a metathesis catalyst system comprising:impregnating a metal oxide on silica support in the presence of a precursor to produce a base catalyst;calcining the base catalyst;dispersing a solid metal-based co-catalyst onto the surface of the base catalyst to produce a doped catalyst; andcalcining the doped catalyst to produce a metathesis catalyst system.2. The method of claim 1 , wherein the large pore silica support comprises large pore silica.3. The method of claim 1 , wherein the co-catalyst is selected from the group consisting of PtO claim 1 , PdCl claim 1 , gamma-AlO claim 1 , or combinations.4. The method of claim 1 , wherein the metal oxide is tungsten oxide.5. The method of claim 1 , wherein the metathesis catalyst system comprises at least 0.5 weight percent (wt. %) co-catalyst.6. The method of claim 1 , wherein the metathesis catalyst system comprises from about 1 wt. % to about 2 wt. % co-catalyst.7. The method of claim 1 , wherein the base catalyst comprises from about 8 wt. % to about 12 wt. % of tungsten oxide.8. The method of claim 1 , wherein the precursor comprises ammonium metatungstate hexahydrate.9. The method of claim 1 , wherein the metathesis catalyst system has a surface area of about 400 m/g to about 800 m/g.10. The method of claim 1 , ...

CATALYST SYSTEMS THAT INCLUDE METAL OXIDE CO-CATALYSTS FOR THE PRODUCTION OF PROPYLENE

Embodiments of methods of synthesizing a metathesis catalyst system, which include impregnating tungsten oxide on silica support in the presence of a precursor to produce a base catalyst; calcining the base catalyst; impregnating a metal oxide co-catalyst comprising a metal oxide onto the surface of the base catalyst to produce a doped catalyst; and calcining the doped catalyst to produce a metathesis catalyst system. Further embodiments of processes for the production of propylene, which include contacting a hydrocarbon feedstock comprising a mixture of 1-butene and 2-butene with embodiments of the metathesis catalyst system to produce, via metathesis conversion, a product stream comprising propylene. 1. A method of synthesizing a metathesis catalyst system comprising:impregnating a metal oxide onto a large pore silica support in the presence of a precursor to produce a base catalyst;calcining the base catalyst;impregnating a metal oxide co-catalyst onto the surface of the base catalyst to produce a doped catalyst; andcalcining the doped catalyst to produce a metathesis catalyst system.2. The method of claim 1 , wherein the large pore silica support comprises an amorphous silica.3. The method of claim 1 , wherein the metal oxide co-catalyst comprises one or more transition metals.4. The method of claim 1 , wherein the metal oxide co-catalyst comprises one or more metals selected from Cu claim 1 , Co claim 1 , Ce claim 1 , Ni claim 1 , Ga claim 1 , Al claim 1 , and Mo.5. The method of claim 1 , wherein the metathesis catalyst system comprises at least 0.5 weight percent (wt. %) metal oxide co-catalyst.6. The method of claim 1 , wherein the metathesis catalyst system comprises from about 0.5 wt. % to about 2.5 wt. % metal oxide co-catalyst.7. The method of claim 1 , wherein the base catalyst comprises from about 8 wt. % to about 12 wt. % tungsten oxide.8. The method of claim 1 , wherein the precursor comprises ammonium metatungstate hexahydrate.9. The method of claim ...

Catalyst systems that include metal co-catalysts for the production of propylene

Embodiments of methods of synthesizing a metathesis catalyst system, which include impregnating tungsten oxide on silica support in the presence of a precursor to produce a base catalyst; calcining the base catalyst; dispersing a solid metal-based co-catalyst onto the surface of the base catalyst to produce a doped catalyst; and calcining the doped catalyst to produce a metathesis catalyst system. Further embodiments of processes for the production of propylene, which include contacting a hydrocarbon feedstock comprising a mixture of 1-butene and 2-butene with embodiments of the metathesis catalyst system to produce, via metathesis conversion, a product stream comprising propylene.

Methods of Preparing a Catalyst Utilizing Hydrated Reagents

A method comprising a) contacting a solvent, a carboxylic acid, and a peroxide-containing compound to form an acidic mixture wherein a weight ratio of solvent to carboxylic acid in the acidic mixture is from about 1:1 to about 100:1; b) contacting a titanium-containing compound and the acidic mixture to form a solubilized titanium mixture wherein an equivalent molar ratio of titanium-containing compound to carboxylic acid in the solubilized titanium mixture is from about 1:1 to about 1:4 and an equivalent molar ratio of titanium-containing compound to peroxide-containing compound in the solubilized titanium mixture is from about 1:1 to about 1:20; and c) contacting a chromium-silica support comprising from about 0.1 wt. % to about 20 wt. % water and the solubilized titanium mixture to form an addition product and drying the addition product by heating to a temperature in a range of from about 50° C. to about 150° C. and maintaining the temperature in the range of from about 50° C. to about 150° C. for a time period of from about 30 minutes to about 6 hours to form a pre-catalyst. 1. A pre-catalyst composition comprising:a titanium-containing compound comprising a carboxylic acid selected from the group consisting of α-hydroxy isobutyric acid, 2,6 pyridine dicarboxylic acid, mandelic acid, derivatives thereof and a combination thereof, a peroxide-containing compound; a chromium-containing compound, a silica support and a solvent, wherein:(i) a weight ratio of solvent to carboxylic acid is from about 1:1 to about 100:1; and(ii) an equivalent molar ratio of titanium-containing compound to carboxylic acid is from about 1:1 to about 1:4.2. The pre-catalyst composition of wherein the silica support comprises from about 0.1 wt. % to about 20 wt. % water.3. The pre-catalyst composition of wherein the silica support is characterized by a surface area of from about 100 m/gram to about 1000 m/gram and a pore volume of from about 1.0 cm/gram to about 2.5 cm/gram.4. The pre- ...

HYDROCRACKING CATALYST AND PROCESS FOR PRODUCING LUBE BASE STOCKS

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

Methods of Preparing a Catalyst Utilizing Hydrated Reagents

A method comprising a) contacting a solvent, a carboxylic acid, and a peroxide-containing compound to form an acidic mixture wherein a weight ratio of solvent to carboxylic acid in the acidic mixture is from about 1:1 to about 100:1; b) contacting a titanium-containing compound and the acidic mixture to form a solubilized titanium mixture wherein an equivalent molar ratio of titanium-containing compound to carboxylic acid in the solubilized titanium mixture is from about 1:1 to about 1:4 and an equivalent molar ratio of titanium-containing compound to peroxide-containing compound in the solubilized titanium mixture is from about 1:1 to about 1:20; and c) contacting a chromium-silica support comprising from about 0.1 wt. % to about 20 wt. % water and the solubilized titanium mixture to form an addition product and drying the addition product by heating to a temperature in a range of from about 50° C. to about 150° C. and maintaining the temperature in the range of from about 50° C. to about 150° C. for a time period of from about 30 minutes to about 6 hours to form a pre-catalyst. 1. A method comprising:contacting (i) a solvent, (ii) a carboxylic acid selected from the group consisting of α-hydroxy isobutyric acid, 2,6 pyridine dicarboxylic acid, mandelic acid, derivatives thereof and a combination thereof; (iii) a peroxide-containing compound; (iv) a titanium-containing compound; (v) a chromium-containing compound; and (vi) a silica support comprising from about 0.1 wt. % to about 20 wt. % water to form a mixture; andspray drying the mixture to form a pre-catalyst powder; wherein:a weight ratio of solvent to carboxylic acid in the mixture is from about 1:1 to about 100:1;an equivalent molar ratio of titanium-containing compound to carboxylic acid in the mixture is from about 1:1 to about 1:4; andan equivalent molar ratio of titanium from the titanium-containing compound to the peroxide-containing compound in the mixture is from about 1:1 to about 1:20.2. The method ...

Methods of Preparing a Catalyst

A method comprising a) drying a support material comprising silica at temperature in the range of from about 150° C. to about 220° C. to form a dried support; b) contacting the dried support with methanol to form a slurried support; c) subsequent to b), cooling the slurried support to a temperature of less than about 60° C. to form a cooled slurried support; d) subsequent to c), contacting the cooled slurried support with a titanium alkoxide to form a titanated support; and e) thermally treating the titanated support by heating to a temperature of equal to or greater than about 150° C. for a time period of from about 5 hours to about 30 hours to remove the methanol and yield a dried titanated support. 1. A method comprising:a) drying a silica support material at temperature in the range of from about 150° C. to about 220° C. to form a dried support;b) contacting the dried support with a solution comprising methanol containing less than 0.1 wt. % water and basic chromium acetate to form a chrominated, slurried support;c) cooling the chrominated, slurried support to a temperature of less than about 60° C. to form a cooled slurried support;d) contacting the cooled slurried support with titanium n-propoxide to form a titanated slurried support;e) thermally treating the titanated slurried support by increasing the temperature of the titanated support to 60° C. to 70° C.;f) prior to complete removal of methanol, contacting the titanated slurried support with water in an amount ranging from about 0.1 moles to about 10 moles per mole of titanium to produce a mixture;g) thermally treating the mixture by heating the mixture to a temperature of about 150° C. to about 220° C. for a time period of from about 5 hours to about 30 hours to form a precatalyst; andh) calcining the precatalyst at a temperature in the range of from about 400° C. to about 1000° C. for a time period of from about 30 minutes to about 24 hours to form a polymerization catalyst.2. The method of wherein the ...

POROUS BODIES WITH ENHANCED PORE ARCHITECTURE

A porous body is provided with enhanced fluid transport properties that is capable of performing or facilitating separations, or performing reactions and/or providing areas for such separations or reactions to take place. The porous body includes at least 80 percent alpha alumina and has a pore volume from 0.3 mL/g to 1.2 mL/g and a surface area from 0.3 m/g to 3.0 m/g. The porous body further includes a pore architecture that provides at least one of a tortuosity of 7.0 or less, a constriction of 4.0 or less and a permeability of 30 mdarcys or greater. The porous body can be used in a wide variety of applications such as, for example, as a filter, as a membrane or as a catalyst carrier. 1. A method for producing a porous body , the method comprising:providing a precursor mixture comprising (i) milled alpha alumina powder having a particle size of 0.1 to 6 microns, (ii) a non-silicate binder, and (iii) a principle burnout material having a particle size of 1-10 microns;forming a predetermined shape; andsubjecting the shape to a heat treatment step in which the shape is sintered to produce the porous body.2. The method of claim 1 , wherein the porous body comprises at least 80 percent alpha alumina and having a pore volume from 0.3 mL/g to 1.2 mL/g claim 1 , a surface area from 0.3 m/g to 3.0 m/g claim 1 , and a pore architecture that provides at least one of a tortuosity of 7 or less claim 1 , a constriction of 4 or less and a permeability of 30 mdarcys or greater.3. The method of claim 1 , wherein the providing the precursor mixture comprises providing a homogenous mixture of the milled alpha alumina powder claim 1 , the non-silicate binder claim 1 , and the principle burnout material.4. The method of claim 1 , wherein the principle burnout material is a granulated polyolefin.5. The method of claim 1 , wherein the granulated polyolefin is one of polyethylene and polypropylene.6. The method of claim 1 , wherein the precursor mixture further comprises at least one of ...

MULTIPLE-STAGE CATALYST SYSTEM FOR SELF-METATHESIS WITH CONTROLLED ISOMERIZATION AND CRACKING

Embodiments of processes and multiple-stage catalyst systems for producing propylene comprising introducing a hydrocarbon stream comprising 2-butene to an isomerization catalyst zone to isomerize the 2-butene to 1-butene, passing the 2-butene and 1-butene to a metathesis catalyst zone to cross-metathesize the 2-butene and 1-butene into a metathesis product stream comprising propylene and C-Colefins, and cracking the metathesis product stream in a catalyst cracking zone to produce propylene. The isomerization catalyst zone comprises a silica-alumina catalyst with a ratio by weight of alumina to silica from 1:99 to 20:80. The metathesis catalyst comprises a mesoporous silica catalyst support impregnated with metal oxide. The catalyst cracking zone comprises a mordenite framework inverted (MFI) structured silica catalyst. 1. A process for production of propylene comprising:introducing a hydrocarbon stream comprising 2-butene to an isomerization catalyst zone to isomerize the 2-butene to 1-butene, where the isomerization catalyst zone comprises a silica-alumina catalyst with a ratio by weight of alumina to silica from 1:99 to 20:80;{'sub': 4', '6, 'passing the 2-butene and 1-butene to a metathesis catalyst zone to cross-metathesize the 2-butene and 1-butene into a metathesis product stream comprising propylene and C-Colefins, where the metathesis catalyst comprises a mesoporous silica catalyst support impregnated with metal oxide; and'}cracking the metathesis product stream in a catalyst cracking zone to produce propylene, where the catalyst cracking zone comprises a mordenite framework inverted (MFI) structured silica catalyst.2. The process of where the silica-alumina catalyst includes a surface area of 200 m/g to 600 m/g.3. The process of where the silica-alumina catalyst has a pore volume of at least 0.60 cm/g.4. The process of where the silica-alumina catalyst comprises an alumina to silica weight ratio between 1:99 and 10:90.5. The process of where the metal oxide ...

EPOXIDATION PROCESS

A method is provided for improving the performance of a silver-based epoxidation catalyst comprising a carrier. The carrier includes at least 80 percent alpha alumina and has a pore volume from 0.3 mL/g to 1.2 mL/g, a surface area from 0.3 m/g to 3.0 m/g, and a pore architecture that provides at least one of a tortuosity of 7 or less, a constriction of 4 or less and a permeability of 30 mdarcys or greater. A catalytic amount of silver and a promoting amount of one or more promoters is disposed on and/or in said carrier. The method further includes the steps of initiating an epoxidation reaction by reacting a feed gas composition containing ethylene and oxygen present in a ratio of from about 3.5:1 to about 12:1, in the presence of the silver-based epoxidation catalyst at a temperature of about 200° C. to about 230° C., and subsequently increasing the temperature either stepwise or continuously. 1. A method of improving the performance of a silver-based epoxidation catalyst comprising a carrier comprising at least 80 percent alpha alumina and having a pore volume from 0.3 mL/g to 1.2 mL/g , a surface area from 0.3 m/g to 3.0 m/g , and a pore architecture that provides at least one of a tortuosity of 7 or less , a constriction of 4 or less and a permeability of 30 mdarcys or greater; a catalytic amount of silver disposed on and/or in said carrier; and a promoting amount of one or more promoters disposed on said carrier; which method further comprises:initiating an epoxidation reaction by reacting a feed gas composition containing ethylene and oxygen present in a ratio of from about 2.5:1 to about 12:1, in the presence of the silver-based epoxidation catalyst at a temperature of about 200° C. to about 230° C.; andsubsequently increasing the temperature either stepwise or continuously.2. The method according to claim 1 , wherein the subsequently increasing step is conducted stepwise.3. The method according to claim 1 , wherein the feed gas composition contains about 20 ...

MESOPOROUS MATERIALS AND PROCESSES FOR PREPARATION THEREOF

A process for preparing a mesoporous material, e.g., transition metal oxide, sulfide, selenide or telluride, Lanthanide metal oxide, sulfide, selenide or telluride, a post-transition metal oxide, sulfide, selenide or telluride and metalloid oxide, sulfide, selenide or telluride. The process comprises providing an acidic mixture comprising a metal precursor, an interface modifier, a hydrotropic or lyotropic ion precursor, and a surfactant; and heating the acidic mixture at a temperature and for a period of time sufficient to form the mesoporous material. A mesoporous material prepared by the above process. A method of controlling nano-sized wall crystallinity and mesoporosity in mesoporous materials. The method comprises providing an acidic mixture comprising a metal precursor, an interface modifier, a hydrotropic or lyotropic ion precursor, and a surfactant; and heating the acidic mixture at a temperature and for a period of time sufficient to control nano-sized wall crystallinity and mesoporosity in the mesoporous material. Mesoporous materials and a method of tuning structural properties of mesoporous materials. 1383-. (canceled)384. A process for preparing a mesoporous material , said process comprising:preparing an acidic mixture by mixing one or more metal precursors, an interface modifier, a hydrotropic or lyotropic ion precursor, and a surfactant;aging the acidic mixture at a temperature and for a period of time sufficient to form a powder, film or gel; andheating the powder, film or gel at a temperature and for a period of time sufficient to form the mesoporous material.385. The process of wherein the mesoporous material comprises an oxide claim 384 , a sulfide claim 384 , a selenide or a telluride of the following:a transition metal selected from the group consisting of Cr, Zr, Nb, Hf and Ta; a Lanthanide selected from the group consisting of Nd, Sm, Ce and Gd; a post-transition metal comprising Sn; or a mixed metal or a solid acid selected from the group ...

Base oil hydrotreating catalyst and process of use

An improved hydrotreating catalyst and process for making a base oil product wherein the catalyst comprises a base extrudate that includes a high nanopore volume amorphous silica alumina (ASA) and a second amorphous silica alumina. The catalyst and process generally involve the use of a base extrudate comprising the high nanopore volume ASA and the second ASA in a catalyst to produce hydrotreated dewaxed base oil products by contacting the catalyst with a hydrocarbon feedstock. The catalyst base extrudate advantageously comprises a first amorphous silica alumina having a pore volume in the 11-20 nm pore diameter range of 0.2 to 1.0 cc/g and a second amorphous silica alumina having a pore volume in the 11-20 nm pore diameter range of 0.02 to 0.2 cc/g, with the base extrudate formed from the amorphous silica alumina and the alumina having a total pore volume in the 2-50 nm pore diameter range of 0.12 to 1.80 cc/g. The catalyst further comprises at least one modifier element from Groups 6 to 10 and Group 14 of the Periodic Table. The catalyst and process provide improved aromatics saturation.

BASE METAL CATALYST FOR TREATMENT OF OZONE AND VOLATILE ORGANIC COMPOUNDS PRESENT IN AIR SUPPLY

Disclosed herein are base metal catalyst devices for removing ozone, volatile organic compounds, and other pollutants from an air flow stream. A catalyst device includes a housing, a solid substrate disposed within the housing, and a catalyst layer disposed on the substrate. The catalyst layer includes a first base metal catalyst at a first mass percent, a second base metal catalyst at a second mass percent, and a support material impregnated with at least one of the first base metal catalyst or the second base metal catalyst. 120-. (canceled)21. A catalyst composition comprising:a first base metal catalyst;a second base metal catalyst; anda support material impregnated with at least one of the first base metal catalyst or the second base metal catalyst, the support material comprising one or more of ceria, alumina, titania, silica, zirconia, metal organic framework, clay, or zeolite.22. The catalyst composition of claim 21 , wherein the first base metal catalyst and the second base metal catalyst are each independently selected from Cu claim 21 , Fe claim 21 , Co claim 21 , Ni claim 21 , Cr claim 21 , Mn claim 21 , Nd claim 21 , Ba claim 21 , Ce claim 21 , La claim 21 , Pr claim 21 , Mg claim 21 , Ca claim 21 , Zn claim 21 , Nb claim 21 , Zr claim 21 , Mo claim 21 , Sn claim 21 , Ta claim 21 , and Sr claim 21 , with the proviso that the first base metal catalyst and the second base metal catalyst are different.23. The catalyst composition of claim 21 , wherein the first base metal catalyst comprises copper oxide claim 21 , and wherein the copper oxide is present from about 1% to about 30% by mass based on a total mass of the catalyst composition.24. The catalyst composition of claim 23 , wherein the second base metal catalyst comprises manganese oxide claim 23 , and wherein the manganese oxide is present from about 1% to about 30% by mass based on a total mass of the catalyst composition.25. The catalyst composition of claim 21 , wherein the support material is an ...

CATALYST COMPOSITE AND USE THEREOF IN THE SELECTIVE CATALYTIC REDUCTION OF NOx

The present invention relates to a process for the preparation of a catalyst for selective catalytic reduction comprising• (i) preparing a mixture comprising a metal-organic framework material comprising an ion of a metal or metalloid selected from groups 2-5, groups 7-9, and groups 11-14 of the Periodic Table of the Elements, and at least one at least monodentate organic compound, a zeolitic material containing a metal as a non-framework element, optionally a solvent system, and optionally a pasting agent,• (ii) calcining of the mixture obtained in (i); and further relates to a catalyst per se comprising a composite material containing an amorphous mesoporous metal and/or metalloid oxide and a zeolitic material, wherein the zeolitic material contains a metal as non-framework element, as well as to the use of said catalyst.

SYNTHESIS OF A MOVNBTE CATALYST HAVING AN INCREASED SPECIFIC SURFACE AND HIGHER ACTIVITY FOR THE OXIDATIVE DEHYDROGENATION OF ETHANE TO ETHYLENE

The invention relates to a mixed oxide material comprising the elements molybdenum, vanadium, niobium and tellurium, which, when using the Cu-Kα radiation, has diffraction reflections h, i, k and l in the XRD spectrum, said diffraction reflexes having their apex points at the diffraction angles (2·) 26.2°±0.5° (h), 27.0°±0.5° (i), 7.8°±0.5° (k) and 28.0°±0.5° (l), characterized in that the mixed oxide material has a pore volume of >0.1 cm/g. The mixed oxide material according to the invention is produced by a method comprising the steps of: a) producing a mixture of starting compounds containing molybdenum, vanadium, niobium and tellurium dioxide as a tellurium-containing starting compound as well as oxalic acid and a further oxoligand selected from the group consisting of dicarboxylic acids and diols, b) hydrothermally treating the mixture of starting compounds at a temperature of 100 to 300° C., c) separating and drying the mixed oxide material which is contained in the suspension resulting from step b). 1. A mixed oxide material comprising the elements molybdenum , vanadium , niobium and tellurium which in the XRD using Cu-Kα radiation has diffraction reflections h , i , k and l whose peaks are approximately at the diffraction angles (2θ) 26.2°±0.5° (h) , 27.0°±0.5° (i) , 7.8°±0.5° (k) and 28.0°±0.5° (l) , charactcrizcd in that wherein the mixed oxide material has a pore volume of greater than 0.1 cm3/g.2. The mixed oxide material as claimed in claim 1 , wherein it has a BET surface area of more than 30 m2/g.3. The mixed oxide material as claimed in claim 1 , wherein it has a volume of the pores smaller than 10 nm of more than 0.2 cm/g.4. The mixed oxide material as claimed in claim 1 , wherein the molar Mo:Te ratio is ≤11 and the molar Mo:Nb ratio is ≤11.5. A process for producing a mixed oxide material as claimed in claim 1 , comprising the steps:a) production of a mixture of starting compounds containing molybdenum, vanadium, niobium and a tellurium-containing ...

HIGH HDN SELECTIVITY HYDROTREATING CATALYST

Improved supported hydroprocessing catalysts, and their method of preparation useful for the hydrodesulfurization (HDS) and hydrodenitrogenation (HDN) of a petroleum feedstock, including a residuum hydrocarbon feedstock are disclosed. The Catalysts contain at least one Groups VIB metal component, at least one Group VIII metal component, and a phosphorus component, supported on a foraminous support such as alumina. The supported catalysts are characterized by a specific combination of properties, namely, the Group VIII metal to Phosphorous molar ratio, the Group VIII metal to Group VIB metal molar ratio, the phosphorous component to Group VIB component molar ratio and the median pore diameter. The resulting catalysts exhibit enhanced HDN without sacrificing to any significant degree the HDS activity. 1. A supported catalyst comprising at least one metal containing catalyst component and at least one phosphorous containing catalyst component , wherein the metal in the metal containing catalyst component is least one selected from Group VIB of the Periodic Table of the Elements , at least one other one metal selected from Group VIII of the Periodic Table of the Elements , and wherein said catalyst components are carried on a foraminous support , said catalyst being characterized as having:(a) a Group VIII metal component to Phosphorous component molar ratio of less than 0.60:1;(b) a Group VIII metal component to Group VIB metal component molar ratio of less than 0.45:1;(c) a phosphorous component to Group VIB metal component molar ratio of greater than 0.23:1; and(d) a median pore diameter of greater than 75 Å and less than 95 Å.2. The catalyst of wherein:(a) the Group VIII metal component to Phosphorous component molar ratio is from about 0.05:1 to about 0.59:1;(b) the Group VIII metal component to Group VIB metal component molar ratio is from about 0.05 to about 0.44:1;(c) the phosphorous component to Group VIB metal component molar ratio is from about 0.24:1 to ...

Extruded Titania-Based Materials Comprising Quaternary Ammonium Compounds and/or Prepared Using Quaternary Ammonium Compounds

Porous, extruded titania-based materials further comprising one or more quaternary ammonium compounds and/or prepared using one or more quaternary ammonium compounds, Fischer-Tropsch catalysts comprising them, uses of the foregoing, processes for making and using the same and products obtained from such processes. 1. A porous , extruded titania-based material further comprising one or more quaternary ammonium compounds.2. A porous claim 1 , extruded titania-based material according to claim 1 , in the form of symmetrical cylinders claim 1 , dilobes claim 1 , trilobes claim 1 , quadralobes or hollow cylinders.3. A porous claim 1 , extruded titania-based material according to claim 1 , having a crush strength of greater than 3.0 lbf claim 1 , preferably greater than 5.0 lbf.4. A porous claim 1 , extruded titania-based material according to claim 1 , wherein the one or more quaternary ammonium compounds comprises tetramethylammonium hydroxide claim 1 , tetraethylammonium hydroxide claim 1 , tetrapropylammonium hydroxide claim 1 , tetrabutylammonium hydroxide or cetyltrimethylammonium hydroxide.5. A porous claim 1 , extruded titania-based material according to claim 1 , comprising mesopores and macropores.6. A porous claim 5 , extruded titania-based material according to claim 5 , wherein the mesopores have a pore diameter of 2 to 50 nm claim 5 , preferably 15 to 45 nm or 30 to 45 nm claim 5 , more preferably 25 to 40 nm or 30 to 40 nm.7. A porous claim 5 , extruded titania-based material according to claim 5 , wherein the macropores have a pore diameter of greater than 50 nm claim 5 , preferably 60 to 1000 nm claim 5 , more preferably 100 to 850 nm.8. A porous claim 5 , extruded titania-based material according to claim 5 , wherein the total pore volume is at least 0.3 ml/g claim 5 , preferably at least 0.40 ml/g.9. A porous claim 5 , extruded titania-based material according to claim 5 , wherein the surface area is at least 30 m/g claim 5 , preferably at least 40 m/g. ...

CATALYST WITH A MESOPOROUS AND MACROPOROUS CO-MIXED NICKEL ACTIVE PHASE HAVING A MEDIAN MACROPORE DIAMETER IN THE RANGE 50 TO 300 NM, AND ITS USE IN HYDROGENATION

A catalyst comprising a calcined oxide matrix which is mainly alumina and an active phase comprising nickel, said active phase being at least partially co-mixed within said calcined oxide matrix which is mainly alumina, the nickel content being in the range 5% to 65% by weight of said element with respect to the total mass of catalyst, said active phase not comprising any metal from group VIB, the nickel particles having a diameter of less than 15 nm, said catalyst having a median mesopore diameter in the range 12 nm to 25 nm, a median macropore diameter in the range 50 to 300 nm, a mesopore volume, measured by mercury porosimetry, of 0.40 mL/g or more and a total pore volume, measured by mercury porosimetry, of 0.45 mL/g or more. The process for the preparation of said catalyst, and its use in a hydrogenation process. 1. A catalyst comprising a calcined oxide matrix which is mainly alumina and an active phase comprising nickel , said active phase being at least partially co-mixed within said calcined oxide matrix which is mainly alumina , the nickel content being in the range 5% to 65% by weight of said element with respect to the total mass of catalyst , said active phase not comprising any metal from group VIB , the nickel particles having a diameter of less than 15 nm , said catalyst having a median mesopore diameter in the range 12 nm to 25 nm , a median macropore diameter in the range 50 to 300 nm , a mesopore volume , measured by mercury porosimetry , of 0.40 mL/g or more and a total pore volume , measured by mercury porosimetry , of 0.45 mL/g or more.2. The catalyst as claimed in claim 1 , in which the macropore volume is in the range 10% to 40% of the total pore volume.3. The catalyst as claimed in claim 1 , in which the nickel content is in the range 10% to 34% by weight of said element with respect to the total mass of catalyst.4. The catalyst as claimed in claim 1 , having no micropores.5. The catalyst as claimed in claim 1 , in which the nickel ...

MIXED OXIDE BASED ON CERIUM AND ZIRCONIUM

A mixed oxide, a catalytic composition, a catalytic wall-flow monolith, the use of the mixed oxide and the process of the preparation of the mixed oxide. The mixed oxide comprises zirconium, cerium, lanthanum and optionally at least one rare earth element other than cerium and other than lanthanum. The catalytic composition and the wall-flow monolith comprise the particles of the mixed oxide. The use of the mixed oxide is in the preparation of a coating on a filter. The process of preparation of the mixed oxide consists jet milling. The mixed oxide is a compromise between a calibrated size and a low viscosity when in the form of an aqueous slurry while retaining a high specific surface area and a high pore volume. 139-. (canceled)43. Mixed oxide according to comprising also hafnium claim 40 , the proportion of hafnium in the mixed oxide being more particularly lower than or equal to 2.5% claim 40 , this proportion being given by weight of oxide relative to the mixed oxide as a whole.44. Mixed oxide according to wherein the proportion of cerium is between 8.0% and 45.0%.45. Mixed oxide according to wherein the proportion of cerium is between 18.0% and 37.0%.46. Mixed oxide according to wherein the proportion of lanthanum is between 1.0% and 15.0%.47. Mixed oxide according to wherein the proportion of the rare earth element(s) is comprised between 0% and 15.0%.48. Mixed oxide according to wherein the proportion of zirconium is higher than 45%.49. Mixed oxide according to comprising a weight ratio ZrO/CeO>1.0.50. Mixed oxide according to wherein d50 is strictly less than 2.5 μm.51. Mixed oxide according to wherein the particles exhibit a d10 lower than or equal to 1.0 μm.52. Mixed oxide according to wherein the particles exhibit a d10 higher than or equal to 0.2 μm.53. Mixed oxide according to wherein the particles exhibit a d99 lower than or equal to 20.0 μm.54. Mixed oxide according to wherein the particles exhibit a d99 higher than or equal to 5.0 μm.55. Mixed oxide ...

DUAL CATALYST SYSTEM FOR PROPYLENE PRODUCTION

Embodiments of processes for producing propylene utilize a dual catalyst system comprising a mesoporous silica catalyst impregnated with metal oxide and a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm/g, and the MFI structured silica catalyst has a total acidity of 0.001 mmol/g to 0.1 mmol/g. The propylene is produced from the butene stream via metathesis by contacting the mesoporous silica catalyst and subsequent cracking by contacting the MFI structured silica catalyst. 1. A process for production of propylene comprising:contacting a stream comprising butene with a metathesis catalyst in a metathesis catalyst zone,passing the stream comprising butene directly from the metathesis catalyst zone to a cracking catalyst zone comprising a cracking catalyst, andcontacting the stream comprising butene with the cracking catalyst in the cracking catalyst zone, where the stream comprising butene contacts the metathesis catalyst before contacting the cracking catalyst.2. The process of where the stream comprising butene includes 2-butene.3. The process of where the stream comprising butene is contacted with the metathesis catalyst and the cracking catalyst at a space hour velocity of from 300 per hour to 1200 per hour.4. The process of where the stream comprising butene is contacted with the metathesis catalyst and the cracking catalyst at a temperature of from 300 degrees Celsius to 600 degrees Celsius and a pressure of from 1 bar to 10 bars.5. The process of where the metathesis catalyst catalyzes isomerization of 2-butene to 1-butene followed by cross-metathesis of 2-butene and 1-butene into a metathesis product stream comprising propylene claim 1 , and the cracking catalyst produces propylene from Cor Colefins in the metathesis product stream.6. The process of where the ...

CATALYSTS CONTAINING SPECIFIC TITANIUM POLYMORPHIC FORMS

A catalyst composition which comprises titanium, wherein part of the titanium is present as a titanium dioxide phase and at least some of the titanium dioxide phase is in the brookite polymorphic form is provided. In some embodiments, the catalyst also comprises a silica support which exhibits a high surface area and pore volume. Methods of preparing the catalyst and its use in an epoxidation reaction are also provided. 2. The catalyst composition of claim 1 , wherein the brookite form of the titanium dioxide phase is present in an amount from about 0.1 wt. % to about 50 wt. % of the titanium dioxide phase.3. The catalyst composition of claim 1 , wherein the catalyst composition has a powder X-ray diffraction spectra comprising peaks at about 25.3 claim 1 , 25.7 claim 1 , 30.8 claim 1 , 36.1 claim 1 , and 48.0 °2θ.4. The catalyst composition of claim 1 , wherein the silica support comprises amorphous silica having:{'sup': '2', '(a) a surface area greater than 800 m/g; and'}{'sup': '3', '(b) a pore volume greater than 1.0 cm/g.'}5. The catalyst composition of claim 1 , wherein the amount of titanium dioxide phase is from about 1 wt. % to about 8 wt. % of the catalyst composition.6. The catalyst composition of claim 1 , further comprising a plurality of organosilicategroups on the surface of the catalyst composition.7. The catalyst composition of claim 6 , wherein the organosilicategroup is —OSi(CH).9. The method of claim 8 , wherein the silica support is dried at a temperature from about 100° C. to about 850° C. for a time period from about 1 hour to about 48 hours.10. The method of claim 8 , wherein the titanium-containing reagent is titanium(IV) alkoxide claim 8 , titanium(IV) halide claim 8 , or a mixed titanium(IV) alkoxide halide.11. The method of claim 10 , wherein the titanium(IV) halide is TiCl.12. The method of claim 11 , wherein the TiClis deposited to the dried silica support as a liquid claim 11 , as a gas claim 11 , or as part of a solution claim 11 , ...

INTEGRATED PROCESS AND SYSTEM TO UPGRADE CRUDE OIL

The processes and systems herein integrate hydroprocessing and coking in a manner to effectively upgrade/desulfurize crude oil feedstocks. An initial liquid hydrocarbon feedstock, such as crude oil, is upgraded by fractionating both the hydrocarbon feedstock and coker thermally cracked hydrocarbon products in a fractionating zone. A coker recycle stream is thermally cracked to produce coker thermally cracked hydrocarbon products that are passed to the fractionating zone. The hydrocarbon distillates are hydroprocessed under conditions effective for desulfurization and conversion into lighter hydrocarbon distillates to produce a hydroprocessed liquid hydrocarbon effluent, such as a bottomless synthetic crude oil. 1. An integrated process for upgrading an initial liquid hydrocarbon feedstock comprising:fractionating both the liquid hydrocarbon feedstock and coker thermally cracked hydrocarbon products in a fractionating zone to separate commingled hydrocarbons into a hydrocarbon distillates stream and a coker recycle stream;thermally cracking the coker recycle stream to produce coker thermally cracked hydrocarbon products that are passed to the fractionating zone; andhydroprocessing the hydrocarbon distillates stream under conditions effective for desulfurization and conversion into lighter hydrocarbon distillates to produce a hydroprocessed liquid hydrocarbon effluent.2. The process of claim 1 , further comprising recovering coke from the coking zone claim 1 , and gasifying at least a portion of the recovered coke in the presence of an oxygen-containing gas to produce hydrogen claim 1 , and recycling at least a portion of the hydrogen to the integrated hydroprocessing step.3. The process of claim 2 , wherein recovered coke is processed into a particulate form effective for gasification before gasifying.4. The process as in claim 1 , wherein thermally cracking is with a delayed coking unit.5. The process as in claim 1 , wherein thermally cracking is with a fluid coking ...

CATALYST SUPPORT AND CATALYSTS PREPARED THEREFROM

A supported catalyst useful in processes for chemically refining hydrocarbon feedstocks is prepared, the catalyst comprising a metal from Group 6 of the Periodic Table, a metal from Groups 8, 9 or 10 and optionally phosphorous, wherein the metals, and phosphorous when present, are carried on a foraminous carrier or support, the carrier or support, preferably comprises porous alumina having a total pore volume (TPV) of about 0.6 cc/g to about 1.1 cc/g and comprising: (a) equal to or greater than about 78% to about 95% of TPV in pores having a diameter of less than about 200 Angstroms (Å); (b) greater than about 2% to less than about 19% of the TPV in pores having a diameter of about 200 (Å) to less than about 1000 Å; (c) equal to or greater than 3% to less than 12% of the TPV in pores having a diameter equal to or greater than about 1000 Å; and (d) a pore mode equal to or greater than about 90 Å and less than about 160 Å. Preferably the support exhibits a d50 greater than about 100 Å and less than about 150 Å. 1. A supported catalyst for treating hydrocarbon feedstocks to produce treated products , said supported catalyst comprising at least one metal from Group 6 , alternatively referred to as Group VIB , of the Periodic Table of the Elements , at least one metal from Groups 8 , 9 or 10 , alternatively referred to as Group VIII , of the Periodic Table of the Elements , and optionally comprising phosphorous , wherein said metals , and phosphorous when present , are carried on a foraminous carrier or support , said carrier or support having a unimodal pore size distribution , a total pore volume (TPV) of about 0.6 cc/g to about 1.1 cc/g and pore size distribution and contents corresponding to values measured by the mercury porosimetry method comprising:(a) equal to or greater than about 78% to about 95% of TPV in pores having a diameter of less than 200 Angstroms (Å);(b) greater than about 2% to less than about 19% of TPV in pores having a diameter of 200 (Å) to less ...

SEMICONDUCTOR PHOTOCATALYST AND PREPARATION METHOD THEREOF

The present invention discloses a novel magnetic BiOCl—BiOCl/MnFeO—FeOsemiconductor photocatalyst as a staggered multi-heterojunction nano-photocatalyst for pharmaceutical effluents remediation, and preparation method and use thereof. The semiconductor photocatalysts are at weighted ratios 9:1 4:1, 7:3 and 3:2 of BiOCl—BiOCland MnFeO—FeOsemiconductor. The BiOCl—BiOCl/MnFeO—FeOsemiconductor photocatalyst with 10% MnFeO—FeOis a solar light activated photocatalyst for pharmaceutical effluents remediation. The pharmaceutical effluents include ofloxacin antibiotic. The mentioned semiconductor photocatalyst effectively removes the ofloxacin (OFL) antibiotic from polluted aqueous solution under simulated solar light, facilitates separation of photocatalyst from treated aqueous solution using magnetic property, enhances light absorption edge, improves intra-particle mass transfer, increases adsorption capacity and promotes efficient surface reactions, which includes: increasing the light absorption range, increasing quantum efficiency and reducing the recombination phenomenon. 1. A method of preparing a semiconductor photocatalyst , comprising:{'sub': 2', '4', '2', '3, 'preparing a mixed phase of MnFeO—FeO; and'}{'sub': 24', '31', '10', '24', '31', '10', '2', '4', '2', '3, 'reacting said mixed phase with a BiOCl—BiOClprecursor phase, to form a staggered multi-heterojunction structure of BiOCl—BiOCl/MnFeO—FeO(BOC-MFO) semiconductor photocatalyst.'}2. The semiconductor photocatalyst of claim 1 , is a solar light activated photocatalyst for pharmaceutical effluents remediation.3. The semiconductor photocatalyst of claim 2 , wherein the pharmaceutical effluents include ofloxacin antibiotic.4. The semiconductor photocatalyst of claim 1 , is in a form of composite nanosheets.5. The semiconductor photocatalyst of claim 1 , is of at least one of the weight ratios of 9:14:1 claim 1 , 7:3 or 3:2.6. The semiconductor photocatalyst of claim 1 , is synthesized through sono-solvothermal ...

ACTIVATED CARBON WITH IMPROVED MECHANICAL RESISTANCE, AND THE USES THEREOF, ESPECIALLY AS A CATALYST CARRIER

The present invention relates to active charcoals with improved mechanical properties. They can advantageously be used in the sweetening of petroleum fractions, as oxidation catalyst support in the conversion of mercaptans to disulphides, but also in any other type of reaction, such as, for example, for the oxidation of cyanide present in water or in the synthesis of glyphosate, and in processes for purification and/or separation by selective adsorption in a liquid phase and/or in a gas phase (decolouration of liquid foodstuffs, water treatment, air treatment, recovery of solvents, and the like). 1. (canceled)2. A method according to claim 13 , said active charcoal characterized in that it exhibits:a micropore volume, measured by nitrogen adsorption, of greater than or equal to 0.20 ml/g,a mesopore volume, measured by nitrogen adsorption and mercury intrusion, of greater than or equal to 0.15 ml/g, anda macropore volume, measured by mercury intrusion, of greater than or equal to 0.40 ml/g.3. A method according to claim 13 , said active charcoal characterized in that its iron content by weight of less than or equal to 2000 ppm.4. A method according to claim 13 , said active charcoal having a bulk density of between 0.20 and 0.50.5. A method according to claim 13 , said active charcoal having an ash content of less than or equal to 10% of the total weight of the active charcoal.6. A method according to claim 13 , said active charcoal particle size such that the charcoal particles are retained by a sieve with a mesh size of 0.2 mm and are provided in the form of strands claim 13 , granules or beads.7. A method according to claim 13 , said active charcoal produced from fruit stones or olive marc.8. (canceled)9. Catalyst for the oxidation of mercaptans to disulphides claim 13 , characterized in that it is composed of at least one metal complex claim 13 , such as a cobalt claim 13 , nickel claim 13 , copper claim 13 , zinc or vanadium phthalocyanine claim 13 , preferably ...

Methods of Preparing a Catalyst Utilizing Hydrated Reagents

A method comprising a) contacting a solvent, a carboxylic acid, and a peroxide-containing compound to form an acidic mixture wherein a weight ratio of solvent to carboxylic acid in the acidic mixture is from about 1:1 to about 100:1; b) contacting a titanium-containing compound and the acidic mixture to form a solubilized titanium mixture wherein an equivalent molar ratio of titanium-containing compound to carboxylic acid in the solubilized titanium mixture is from about 1:1 to about 1:4 and an equivalent molar ratio of titanium-containing compound to peroxide-containing compound in the solubilized titanium mixture is from about 1:1 to about 1:20; and c) contacting a chromium-silica support comprising from about 0.1 wt. % to about 20 wt. % water and the solubilized titanium mixture to form an addition product and drying the addition product by heating to a temperature in a range of from about 50° C. to about 150° C. and maintaining the temperature in the range of from about 50° C. to about 150° C. for a time period of from about 30 minutes to about 6 hours to form a pre-catalyst. 1. A method comprising:a) contacting a solvent, a carboxylic acid, and a peroxide-containing compound to form an acidic mixture wherein a weight ratio of solvent to carboxylic acid in the acidic mixture is from about 1:1 to about 100:1;b) contacting a titanium-containing compound and the acidic mixture to form a solubilized titanium mixture wherein an equivalent molar ratio of titanium-containing compound to carboxylic acid in the solubilized titanium mixture is from about 1:1 to about 1:4 and an equivalent molar ratio of titanium-containing compound to peroxide-containing compound in the solubilized titanium mixture is from about 1:1 to about 1:20; andc) contacting a chromium-silica support comprising from about 0.1 wt. % to about 20 wt. % water and the solubilized titanium mixture to form an addition product and drying the addition product by heating to a temperature in a range of from ...

EXHAUST GAS PURIFICATION CATALYST AND PRODUCTION METHOD THEREOF

An exhaust gas purification catalyst contains an oxide 1 and an oxide 2. The catalyst has pores Pwith a pore size of from 1 nm to 260 nm, that can be measured by the nitrogen absorption method, and the total sum ΣPVof the pore volume PVof the pores is equal to or greater than 0.79 cm/g. 19.-. (canceled)12. The exhaust gas purification catalyst according to claim 10 , wherein the oxide 1 contains cerium (Ce) and/or zirconium (Zr).13. The exhaust gas purification catalyst according to claim 11 , wherein the oxide 1 contains cerium (Ce) and/or zirconium (Zr).14. The exhaust gas purification catalyst according to claim 10 , wherein the oxide 1 is a complex oxide that contains cerium (Ce) and/or zirconium (Zr).15. The exhaust gas purification catalyst according to claim 11 , wherein the oxide 1 is a complex oxide that contains cerium (Ce) and/or zirconium (Zr).16. A method of producing the exhaust gas purification catalyst of claim 10 , comprising the steps of:mixing a precursor of the oxide 2 with the oxide 1 before calcining the oxide 1, and then calcining a resultant mixture.17. The method of producing the exhaust gas purification catalyst according to claim 16 , wherein the precursor of the oxide 2 is a carboxylate of lanthanum (La) and at least one element selected from the group consisting of barium (Ba) claim 16 , strontium (Sr) claim 16 , calcium (Ca) claim 16 , iron (Fe) claim 16 , cobalt (Co) claim 16 , nickel (Ni) and manganese (Mn). The present invention relates to an exhaust gas purification catalyst and a production method thereof, particularly to an exhaust gas purification catalyst with adequate pore volume and good gas diffusion property and a production method thereof.Exhaust gas purification catalysts with an improved redox function have been known in which an oxygen storage material (OSC material) supports LaMM′Ox (M being Ba, Sr, Ca or the like, and M′ being Fe, Co, Ni, Mn or the like) (e.g. see Patent Document 1).Patent Document 1: WO 2012/ ...

MAGANESE OXIDE BASED CATALYST AND CATALYST DEVICE FOR THE REMOVAL OF FORMALDEHYDE AND VOLATILE ORGANIC COMPOUNDS

Disclosed herein are a catalyst composition, catalyst devices, and methods for removing formaldehyde, volatile organic compounds, and other pollutants from an air flow stream. The catalyst composition including manganese oxide, optionally one or more of alkali metals, alkaline earth metals, zinc, iron, binder, an inorganic oxide, or carbon. 1. A catalyst composition comprising:manganese oxide;bentonite; anda polymer binder,wherein the catalyst composition is adapted to remove one or more of formaldehyde, ozone, carbon monoxide, nitrogen oxide, amines, sulfur compounds, thiols, chlorinated hydrocarbons, or volatile organic compounds from an unpurified air supply, and wherein a BJH pore volume of the catalyst composition ranges from about 0.3 mL/g to about 1.5 mL/g.2. The catalyst composition of claim 1 , wherein the polymer binder is selected from a group consisting of polyethylene claim 1 , polypropylene claim 1 , polyolefin copolymers claim 1 , polyisoprene claim 1 , polybutadiene claim 1 , polybutadiene copolymers claim 1 , chlorinated rubber claim 1 , nitrile rubber claim 1 , polychloroprene claim 1 , ethylene-propylene-diene elastomers claim 1 , polystyrene claim 1 , polyacrylate claim 1 , polymethacrylate claim 1 , polyacrylonitrile claim 1 , poly(vinyl esters) claim 1 , poly(vinyl halides) claim 1 , polyamides claim 1 , cellulosic polymers claim 1 , polyimides claim 1 , acrylics claim 1 , vinyl acrylics claim 1 , styrene acrylics claim 1 , polyvinyl alcohols claim 1 , thermoplastic polyesters claim 1 , thermosetting polyesters claim 1 , poly(phenylene oxide) claim 1 , poly(phenylene sulfide) claim 1 , poly(tetrafluoroethylene) claim 1 , polyvinylidene fluoride claim 1 , poly(vinlyfluoride) claim 1 , ethylene chlorotrifluoroethylene copolymer claim 1 , polyamide claim 1 , phenolic resins claim 1 , polyurethane claim 1 , acrylic/styrene acrylic copolymer latex claim 1 , silicone polymers claim 1 , and combinations thereof.3. The catalyst composition of claim 1 , ...

Method for producing transition alumina catalyst monoliths

A method for producing a three-dimensional porous transition alumina catalyst monolith of stacked catalyst fibers, comprising the following steps: a) Preparing a suspension paste in a liquid diluent of hydroxide precursor particles or oxyhydroxide precursor particles of transition alumina particles or mixtures thereof and which suspension can furthermore comprise a binder material in a maximum amount of 20 wt %, based on the amount of hydroxide precursor particles or oxyhydroxide precursor particles of transition alumina particles or mixtures thereof and/or a plasticizer and/or a dopant in a maximum amount of 10 wt %, based on the amount of hydroxide precursor particles or oxyhydroxide precursor particles of transition alumina particles or mixtures thereof, all particles in the suspension having a number average particle size in the range of from 0.05 to 700 μm, b) extruding the paste of step a) through one or more nozzles to form fibers, and depositing the extruded fibers to form a three-dimensional porous catalyst monolith precursor, c) drying the porous catalyst monolith precursor to remove the liquid diluent, d) performing a temperature treatment of the dried porous catalyst monolith precursor of step c) at a temperature in the range of from 500 to 1000° C., to form the transition alumina catalyst monolith, wherein no temperature treatment of the porous catalyst monolith precursor or porous catalyst monolith at temperatures above 1000° C. is performed and wherein no further catalytically active metals, metal oxides or metal compounds are applied to the surface of the transition alumina precursor particles, the catalyst monolith precursor or transition alumina catalyst monolith. no further catalytically active metals, metal oxides or metal compounds are present in the suspension paste.

Spheroidal Resid Hydrodemetallation Catalyst

Spheroidal catalyst support, supported catalyst, and method of preparing and using the catalyst for hydrodemetallation of metal-containing heavy oil feedstocks are disclosed. The catalyst supports comprise titania alumina having 5 wt % or less titania and have greater than 30% percent of their pore volume in pores having a diameter of between 200 and 500 Å. Catalysts prepared from the supports contain Group 6, 9 and 10 metals or metal compounds supported on the titania alumina supports. Catalysts in accordance with the invention exhibit improved catalytic activity and stability to remove metals from heavy feedstocks during a hydrotreating process. The catalysts also provide increased sulfur and MCR conversion during a hydrotreating process. 134-. (canceled)35. A spheroidal catalyst support comprising co-precipitated titania alumina having less than 5 wt % titania based on the total titania alumina , said support having a total pore volume in the range of about 0.7 to about 1.2 cc/g , and a pore volume distribution such that greater than 40% of the total pore volume have pores in a diameter larger than 200 Å , about 30% or greater of the total pore volume have pores in the range of about 200 Å to about 500 Å and , greater than 10% of the total pore volume have pores with a diameter above 1000 Å.36. The support of having a total pore volume in the range of about 0.8 to about 1.1 cc/g.37. The support of wherein titania is present in the co-precipitated titania alumina in an amount ranging from about 2.5 to about 4.0 wt % titania claim 35 , based on the total weight of the titania alumina.38. The support of wherein the support comprises at least 90 wt % titania alumina having an alumina R value of from about 0.4 to about 1.7 claim 35 , wherein R is the ratio between the integrated intensity of the X-ray diffraction peak at 2Θ=32° and the integrated intensity of the X-ray diffraction peak at 2Θ=46°.39. The support of wherein from about 50% to about 90% of the total pore ...

ETHYLENE GAS PHASE POLYMERISATION PROCESS

The invention relates to a gas phase polymerisation process for the production of ethylene polymers in the presence of a catalyst composition based on a chromium compound, a titanium compound and a silica support material. The silica support material has a surface area (SA) between 685 m/g and 800 m/g, a pore volume (PV) between 1.65 and 1.85 cm/g and an average particle size in the range between 25 and 35 micrometres. The catalyst composition is injected by a dry catalyst feeder into the polymerization reactor. 1. A gas phase polymerisation process for the production of ethylene polymers , comprising: polymerizing ethylene in the presence of a catalyst composition based on a chromium compound , a titanium compound and a silica support material characterized in that the silica support material has a surface area (SA) ≥685 m/g and ≤800 m/g , a pore volume (PV) ≥1.65 and ≤1.85 cm/g and an average particle size in the range ≥25 and ≤35 micrometres.2. The process according to claim 1 , wherein the catalyst composition does not comprise a magnesium compound.3. The process according to claim 1 , wherein the surface area (SA) ≥700 m/g.4. The process according to claim 1 , wherein the pore volume (PV) is ≥1.7 cm/g.5. The process according to claim 1 , wherein the average particle size is ≥33 micrometres.6. The process according to claim 1 , wherein the catalyst composition is injected by a dry catalyst feeder into the polymerization reactor.7. The process according to claim 1 , wherein the catalyst composition is a dry catalyst composition.8. The process according to claim 1 , wherein the polymerization of ethylene takes place in a gas phase polymerization in the presence of a comonomer.9. The process according to claim 8 , wherein the comonomer is 1-hexene.10. The process according to claim 1 , wherein the ethylene polymer has high load melt index (HLMI) ≥2 g/10 min and ≤10 g/10 min (HLMI determined using the procedures of ASTM D-1238 Condition F using a load of 21.6 kg at ...

Catalyst For Catalytic Oxidation Treatment Of Organic Wastewater, Preparation Method Thereof, And Application Thereof

A catalyst for catalytic oxidation treatment of organic wastewater, comprising aluminum oxide, and nickel, ferrum, manganese, and cerium supported on the aluminum oxide in oxide form. Based on the weight of aluminum oxide, the contents of the following components in the catalyst are: nickel: 5.0-20 wt %; ferrum: 0.5-5.5 wt %; manganese: 0.5-3.5 wt %; and cerium: 1.5-3.0 wt %. The present invention has a good effect in catalytic oxidation for degrading COD organic pollutants in wastewater and has high reactivity. 1. A catalyst for catalytic oxidation treatment of organic wastewater , wherein the catalyst comprises alumina and nickel , iron , manganese and cerium loaded on the alumina in oxide form; based on the weight of the alumina , the contents of the following components in the catalyst are as follows:nickel 5.0-20 wt %, preferably 5.5-12.0 wt %;iron 0.5-5.5 wt %, preferably 1.5-5.0 wt %;manganese 0.5-3.5 wt %, preferably 1.0-3.0 wt %;cerium 1.5-3.0 wt %, preferably 2.0-2.8 wt %.2. The catalyst according to claim 1 , wherein the catalyst comprises a cerium-modified alumina carrier and nickel claim 1 , iron claim 1 , manganese and cerium loaded on the cerium-modified alumina carrier in oxide form; the cerium-modified alumina carrier comprises alumina and cerium loaded on the alumina in oxide form; based on the weight of the alumina claim 1 , the cerium content of the cerium-modified alumina carrier is 1.0-2.0 wt % claim 1 , preferably 1.2-1.5 wt %.3. The catalyst according to claim 2 , wherein based on the weight of the alumina claim 2 , the content of cerium loaded on the cerium-modified alumina carrier in the catalyst is 0.5-2.0 wt % claim 2 , preferably 0.6-1.5 wt %.4. The catalyst according to claim 1 , wherein the nickel claim 1 , iron claim 1 , manganese and cerium are respectively derived from one or more of nitrates claim 1 , acetates and carbonates containing corresponding metal elements claim 1 , preferably nitrates.5. A preparation method of a catalyst ...

MESOPOROUS SILICA SUPPORTED CATALYST FOR OXIDATIVE DEHYDROGENATION

Oxidative dehydrogenation catalysts comprising bismuth and nickel oxides impregnated on mesoporous silica supports such as SBA-15 and mesoporous silica foam. Methods of preparing and characterizing the catalysts as well as processes for oxidatively dehydrogenating n-butane to butadiene using the catalysts are also described. The disclosed catalysts demonstrate higher n-butane conversion and butadiene selectivity than catalysts supported by conventional silica. 1: A catalyst , comprising:a mesoporous silica support which is at least one selected from the group consisting of SBA-15 and mesoporous silica foam; anda catalytic material comprising nickel oxide and bismuth oxide impregnated on the mesoporous silica support;wherein the nickel and bismuth atoms of the nickel oxide and the bismuth oxide are present in amounts of 2-30 wt % and 5-40 wt %, each relative to a weight of the mesoporous silica support.2: The catalyst of claim 1 , wherein the mesoporous silica support has a pore volume of 0.2-3 cm/g and a BET surface area of 200-1 claim 1 ,000 m/g.3: The catalyst of claim 1 , wherein the mesoporous silica support is SBA-15.4: The catalyst of claim 1 , wherein 50-99.9 wt % of the bismuth oxide is present as a non-stoichiometric bismuth oxide relative to a total weight of the bismuth oxide.5: The catalyst of claim 4 , wherein the non-stoichiometric bismuth oxide has a formula of BiO claim 4 , in which x ranges from 0.2 to 0.4.6: The catalyst of claim 1 , which has an average pore diameter of 2-20 nm.7: The catalyst of claim 1 , which has a pore volume of 0.2-2 cm/g.8: The catalyst of claim 1 , which has a BET surface area of 200-700 m/g.9: A method of preparing the catalyst of claim 1 , the method comprising:mixing the mesoporous silica support with an aqueous solution comprising a nickel salt and a bismuth salt to form a mixture;drying the mixture to form a dried mass; andcalcining the dried mass in air at a temperature of 300-700° C. thereby producing the catalyst.10 ...

PHOTO-REDOX TITANIUM CONTAINING ORGANIC FRAMEWORKS AND METHODS OF MAKING AND USE THEREOF

Disclosed herein are metal-organic frameworks and methods of making and use thereof. 2. The metal-organic framework of claim 1 , wherein Rand Rare independently selected from H claim 1 , unsubstituted linear or branched C-Calkyl claim 1 , and unsubstituted C-Ccycloalkyl.3. The metal-organic framework of or claim 1 , wherein Ris H and Ris selected from the group consisting of unsubstituted linear or branched C-Calkyl and unsubstituted C-Ccycloalkyl.4. The metal-organic framework of any one of - claim 1 , wherein Ris H and Ris selected from the group consisting of methyl claim 1 , ethyl claim 1 , isopropyl claim 1 , n-butyl claim 1 , cyclopentyl claim 1 , cyclohexyl claim 1 , and n-heptyl.5. The metal-organic framework of any one of - claim 1 , wherein the titanium oxide clusters comprise TiOring shaped clusters.7. The metal-organic framework of claim 6 , wherein Rand Rare independently selected from H claim 6 , unsubstituted linear or branched C-Calkyl claim 6 , and unsubstituted C-Ccycloalkyl.8. The metal-organic framework of or claim 6 , wherein Ris H and Ris selected from the group consisting of unsubstituted linear or branched C-Calkyl and unsubstituted C-Ccycloalkyl.9. The metal-organic framework of any one of - claim 6 , wherein Ris H and Ris selected from the group consisting of methyl claim 6 , ethyl claim 6 , isopropyl claim 6 , n-butyl claim 6 , cyclopentyl claim 6 , cyclohexyl claim 6 , and n-heptyl.10. The metal-organic framework of any one of - claim 6 , wherein the metal-organic framework has a crystal structure in the high symmetry tetragonal I4/mmm space group with low residuals.11. The metal-organic framework of any one of - claim 6 , wherein the metal-organic framework has a BET surface area of from 100 m/g to 2000 m/g.12. The metal-organic framework of any one of - claim 6 , wherein the metal-organic framework has a BET surface area of from 200 m/g to 1000 m/g.13. The metal-organic framework of any one of - claim 6 , wherein the metal-organic ...

METHODS OF PRODUCING ORGANOSILICA MATERIALS AND USES THEREOF

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

Extruded Titania-Based Materials Comprising Quaternary Ammonium Compounds and/or Prepared Using Quaternary Ammonium Compounds

Porous, extruded titania-based materials further comprising one or more quaternary ammonium compounds and/or prepared using one or more quaternary ammonium compounds, Fischer-tropsch catalysts comprising them, uses of the foregoing, processes for making and using the same and products obtained from such processes. 1. A porous , extruded titania-based material further comprising one or more quaternary ammonium compounds.2. A porous claim 1 , extruded titania-based material according to claim 1 , in the form of symmetrical cylinders claim 1 , dilobes claim 1 , trilobes claim 1 , quadralobes or hollow cylinders.3. A porous claim 1 , extruded titania-based material according to claim 1 , having a crush strength of greater than 3.0 lbf claim 1 , preferably greater than 5.0 lbf.4. A porous claim 1 , extruded titania-based material according to claim 1 , wherein the one or more quaternary ammonium compounds comprises tetramethylammonium hydroxide claim 1 , tetraethylammonium hydroxide claim 1 , tetrapropylammonium hydroxide claim 1 , tetrabutylammonium hydroxide or cetyltrimethylammonium hydroxide.5. A porous claim 1 , extruded titania-based material according to claim 1 , comprising mesopores and macropores.6. A porous claim 5 , extruded titania-based material according to claim 5 , wherein the mesopores have a pore diameter of 2 to 50 nm claim 5 , preferably 15 to 45 nm or 30 to 45 nm claim 5 , more preferably 25 to 40 nm or 30 to 40 nm.7. A porous claim 5 , extruded titania-based material according to claim 5 , wherein the macropores have a pore diameter of greater than 50 nm claim 5 , preferably 60 to 1000 nm claim 5 , more preferably 100 to 850 nm.8. A porous claim 5 , extruded titania-based material according to claim 5 , wherein the total pore volume is at least 0.3 ml/g claim 5 , preferably at least 0.40 ml/g.9. A porous claim 5 , extruded titania-based material according to claim 5 , wherein the surface area is at least 30 m/g claim 5 , preferably at least 40 m/g. ...

MESOPOROUS MIXED OXIDE CATALYST COMPRISING SILICON

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

CATALYST Ta-Nb FOR THE PRODUCTION OF 1,3-BUTADIENE

The invention relates to a catalyst that comprises a mesoporous oxide matrix, with said matrix comprising at least one oxide of an element X that is selected from among silicon and titanium, taken by itself or in a mixture, with said catalyst comprising at least the tantalum element and the niobium element, with the tantalum mass representing between 0.1 to 30% by weight of the mass of the mesoporous oxide matrix, the niobium mass representing between 0.02 to 6% by weight of the mass of the mesoporous oxide matrix, the content by mass of the tantalum element being greater than or equal to the content by mass of the niobium element. The invention also relates to the use of this catalyst in a method for the production of 1,3-butadiene from a feedstock that comprises at least ethanol. 1. Catalyst that comprises a mesoporous oxide matrix , with said matrix comprising at least one oxide of an element X that is selected from among silicon and titanium , taken by itself or in a mixture , with said catalyst comprising tantalum and niobium , the tantalum mass representing from 0.1 to 30% of the mass of the mesoporous oxide matrix , the niobium mass representing from 0.02 to 6% of the mass of the mesoporous oxide matrix , the content by mass of the tantalum element in said catalyst being greater than or equal to the content by mass of the niobium element in said catalyst , with said catalyst being prepared by consecutive introduction of the niobium element and then the tantalum element.2. Catalyst according to claim 1 , in which said oxide matrix is mesostructured.3. Catalyst according to claim 1 , in which said oxide matrix is a silicon oxide that has a specific surface area of 100 to 1 claim 1 ,200 m/g claim 1 , a mesopore volume of between 0.2 and 1.8 ml/g and a mesopore diameter of between 4 and 50 nm.4. Catalyst according to claim 3 , in which said oxide matrix contains an alkaline metal content that is expressed in terms of % by weight of metal in relation to the mass ...

STABILIZED PRODUCTION OF 1,3-BUTADIENE IN THE PRESENCE OF A TANTALUM OXIDE DOPED BY AN ALDOLIZING ELEMENT

The invention relates to a catalyst that comprises at least the tantalum element, at least an aldolizing element and at least a mesoporous oxide matrix, with the tantalum mass being between 0.1 and 30% of the mesoporous oxide matrix mass, the mass of the at least one aldolizing element being between 0.02 and 4% of the mesoporous oxide matrix mass, and use thereof. 1. Catalyst that comprises at least the tantalum element , at least an aldolizing element that is selected from the group that consists of magnesium , calcium , barium , cerium and tin and mixtures thereof , and at least one mesoporous oxide matrix that comprises at least one oxide of an element X that is selected from among silicon , titanium and mixtures thereof , with the tantalum element mass being between 0.1 and 30% of the mesoporous oxide matrix mass , and the aldolizing element mass being between 0.02 and 4% of the mesoporous oxide matrix mass.2. Catalyst according to claim 1 , in which said aldolizing element is selected from the group that consists of calcium and barium and mixtures thereof.3. Catalyst according to claim 1 , also comprising at least one element that is selected from the group that consists of the elements of groups 1 claim 1 , 4 and 5 of the periodic table claim 1 , with the mass of said element representing between 0.01 and 5% of the mesoporous oxide matrix mass.4. Catalyst according to claim 3 , also comprising at least one element that is selected from the group that consists of the element Cs and the element Nb and mixtures thereof claim 3 , with the mass of said element representing between 0.01 and 5% of the mesoporous oxide matrix mass.5. Catalyst according to claim 1 , in which said oxide matrix is mesostructured.6. Catalyst according to claim 1 , in which said mesoporous oxide matrix comprises a silicon oxide that has a specific surface area of 100 to 1 claim 1 ,200 m/g claim 1 , a mesopore volume of between 0.2 and 1.8 ml/g claim 1 , and a mesopore diameter of between 4 ...

CERIUM OXIDE PARTICLES AND METHOD FOR PRODUCTION THEREOF

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

Method For Treating Reverse Osmosis Concentrated Water

A method for treating reverse osmosis concentrated water, comprises adding a precipitant and oxidant to reverse osmosis concentrated water for treatment, filtering to obtain clear liquid, and adding catalyst for water treatment to clear liquid for catalytic oxidation to obtain a first-stage treated water. Optionally, the liquid may be subjected after catalytic oxidation to an adsorption treatment; performing reverse osmosis treatment on first-stage treated water to obtain second-stage reverse osmosis product water and second-stage reverse osmosis concentrated water; and adding oxidant to second-stage reverse osmosis concentrated water for oxidation treatment to obtain directly discharged effluent water. The obtaining of effluent water may further comprise subjecting liquid after oxidation treatment to adsorption treatment. The above method can recycle 75-85 wt % of water, and operates easily. Thereby, improvement to overall utilization rate of water, and treatment of little remaining water is met to effluent standard for reduction of environmental pollution and economic investment. 1. A treating method of reverse osmosis concentrated water , characterized in that , comprising the following steps:(1) adding a precipitant and an oxidant to reverse osmosis concentrated water for treatment, filtering to obtain a clear liquid, and adding a catalyst for water treatment to the clear liquid for catalytic oxidation to obtain first-stage treated water; wherein the obtaining of the first-stage treated water optionally further comprises subjecting the liquid after catalytic oxidation to an adsorption treatment;(2) performing reverse osmosis treatment on the first-stage treated water obtained in step (1), to obtain second-stage reverse osmosis product water and second-stage reverse osmosis concentrated water, wherein the second-stage reverse osmosis product water is used for recycling;(3) adding an oxidant to the second-stage reverse osmosis concentrated water obtained in step ( ...

SPHEROIDAL RESID HYDRODEMETALLATION CATALYST

Spheroidal catalyst support, supported catalyst, and method of preparing and using the catalyst for hydrodemetallation of metal-containing heavy oil feedstocks are disclosed. The catalyst supports comprise titania alumina having 5 wt % or less titania and have greater than 30% percent of their pore volume in pores having a diameter of between 200 and 500 Å. Catalysts prepared from the supports contain Group 6, 9 and 10 metals or metal compounds supported on the titania alumina supports. Catalysts in accordance with the invention exhibit improved catalytic activity and stability to remove metals from heavy feedstocks during a hydrotreating process. The catalysts also provide increased sulfur and MCR conversion during a hydrotreating process. 1. A process for preparing a spheroidal support material for supporting catalytically active metals suitable for the hydrodemetallation of heavy hydrocarbon fractions containing metals under hydrotreating conditions , which process comprises:(a) forming a co-precipitated titania alumina containing 5 wt % or less titania, based on the total weight of the titania alumina;(b) peptizing the titania alumina to form an aqueous slurry containing from about 20% to about 35% solids and having a sufficient viscosity to form droplets;(c) dropping the slurry in a dripping column to form spheroidal shaped particles;(d) calcining the spheroidal shaped particles at a temperature ranging from about 960° C. to 1100° C. to obtain a spheroidal titania alumina support having a total pore volume in the range of from about 0.7 to about 1.2 cc/g, and a pore volume distribution such that greater than 40% of the total pore volume having pores in a diameter larger than 200 Å, 30% or greater of the total pore volume having pores in the range of about 200 Å to about 500 Å and, greater than 10% of the total pore volume having pores with a diameter above 1000 Å.2. The process of wherein the titania alumina of the support comprises at least 90 wt % alumina ...

CATALYST, CATALYST LAYER, MEMBRANE-ELECTRODE ASSEMBLY, ELECTROCHEMICAL DEVICE, AND METHOD FOR PRODUCING CATALYST

A catalyst includes a mesoporous material and catalytic metal particles supported at least within the mesoporous material and containing platinum and a metal different from platinum. The mesoporous material has mesopores with a mode radius of 1 to 25 nm and a pore volume of 1.0 to 3.0 cm/g before supporting of the catalytic metal particles, and has an average particle size of greater than or equal to 200 nm. A molar ratio of the metal different from platinum and contained in the catalytic metal particles relative to all metals contained in the catalytic metal particles is greater than or equal to 0.25, and among the catalytic metal particles, a volume ratio of catalytic metal particles having a particle size of greater than or equal to 20 nm is less than or equal to 10%. 1. A catalyst comprising:a mesoporous material; andcatalytic metal particles supported at least within the mesoporous material and containing platinum and a metal different from platinum,{'sup': 3', '3, 'wherein the mesoporous material has mesopores with a mode radius of greater than or equal to 1 nm and less than or equal to 25 nm and a pore volume of greater than or equal to 1.0 cm/g and less than or equal to 3.0 cm/g before supporting of the catalytic metal particles, and has an average particle size of greater than or equal to 200 nm,'}a molar ratio of the metal different from platinum and contained in the catalytic metal particles relative to all metals contained in the catalytic metal particles is greater than or equal to 0.25, and among the catalytic metal particles, a volume ratio of catalytic metal particles having a particle size of greater than or equal to 20 nm is less than or equal to 10%.2. The catalyst according to claim 1 , wherein a molar ratio of the metal different from platinum and contained in the catalytic metal particles having a particle size of greater than or equal to 20 nm relative to all metals contained in the catalytic metal particles having a particle size of greater ...

FISCHER-TROPSCH CATALYSTS

The invention relates to the preparation of a Fischer-Tropsch catalyst support and of a Fischer-Tropsch catalyst. A silica comprising support is subjected to hydrothermal treatment. The hydrothermal treatment results in catalysts having improved C+ selectivity as compared with catalysts prepared with a non-treated silica comprising support. 1. A process for performing a Fischer Tropsch reaction comprising the following steps:providing a reactor with a Fischer-Tropsch catalyst manufactured according to a process comprising the steps of:providing a catalyst support material comprising silica;subjecting the catalyst support material to hydrothermal treatment wherein the hydrothermal treatment is performed using a monoethanolamine comprising solution with a pH in the range of between 7 and 11, or using a monoethanolamine and nitric acid comprising solution with a pH in the range of between 7 and 11; andin which process the catalyst support material is shaped before or after the hydrothermal treatment;providing syngas to the reactor and providing the following process conditions in the reactor: a temperature in the range from 125 to 350° C., a pressure in the range from 5 to 150 bar absolute, and a gaseous hourly space velocity in the range from 500 to 10000 Nl/l/h;removing Fischer Tropsch product from the reactor.2. The process for performing a Fischer Tropsch reaction according to wherein the process for manufacturing the Fischer-Tropsch catalyst further comprises the step of:impregnating the shaped treated catalyst support material with a catalytically active metal.3. The process for performing a Fischer Tropsch reaction according to wherein the process for manufacturing the Fischer-Tropsch catalyst further comprises the step of:subjecting the obtained catalyst to hydrogen or a hydrogen-containing gas.4. The process for performing a Fischer Tropsch reaction according to claim 1 , wherein in process for manufacturing the Fischer-Tropsch catalyst the catalyst support ...

METHOD FOR PRODUCING POROUS CARBON, AND ELECTRODE AND CATALYST SUPPORT CONTAINING POROUS CARBON PRODUCED BY SAID PRODUCTION METHOD

A method of producing a porous carbon is provided that can change type of functional groups, amount of functional groups, or ratio of functional groups while inhibiting its pore structure from changing. A method of producing a porous carbon includes: a first step of carbonizing a material containing a carbon source and a template source, to prepare a carbonized product; and a second step of immersing the carbonized product into a template removing solution, to remove a template from the carbonized product, and the method is characterized by changing at least two or more of the following conditions: type of the material, ratio of the carbon source and the template source, size of the template, and type of the template removal solution, to thereby control type, amount, or ratio of functional groups that are present in the porous carbon. 1. A method of producing a porous carbon , comprising:a first step of carbonizing a material containing a carbon source and a template source, to prepare a carbonized product; and a second step of immersing the carbonized product into a template removing solution, to remove a template from the carbonized product, the method characterized by:changing at least two or more of the following conditions: type of the material, ratio of the carbon source and the template source, size of the template, and type of the template removal solution, to thereby control type, amount, or ratio of functional groups that are present in the porous carbon.2. The method of producing a porous carbon according to claim 1 , further comprising:after the second step, a third step of heat-treating the carbonized product from which the template has been removed; and changing at least two or more of the following conditions including temperature or time of the heat treatment, in addition to type of the material, ratio of the carbon source and the template source, size of the template, ad type of the template removal solution, to thereby control type, amount, or ...

Hydrocracking Catalyst and Use of the Same

A hydrocracking catalyst comprises a support, at least one of VIII Group metal components, and at least one of VIB Group metal components. The support comprises an acidic silica-alumina component and alumina derived from a pseudo-boehmite component, wherein the content of the acidic silica-alumina component is 3-80 wt %, the content of alumina derived from the pseudo-boehmite component is 20-95 wt %, based on the support. The support is obtained by mixing, moulding, drying and calcining the acidic silica-alumina component with the pseudo-boehmite component, wherein said pseudo-boehmite component comprises pseudo-boehmite PB1 and pseudo-boehmite PB2, wherein the content of PB1 is 10-90 wt % and the content of PB2 is 0-60 wt % on a dry basis and based on the support. 1. A hydrocracking catalyst , comprising a support and at least one of VIII Group metal components and at least one of VIB Group metal components , wherein said support comprises an acidic silica-alumina component and alumina derived from a pseudo-boehmite component , wherein the content of the acidic silica-alumina component is 3-80 wt % , the content of alumina derived from the pseudo-boehmite component is 20-95 wt % , based on the support , characterized in that said support is obtained by mixing , moulding , drying and calcining the acidic silica-alumina component with the pseudo-boehmite component , wherein said pseudo-boehmite component comprises pseudo-boehmite PB1 and pseudo-boehmite PB2 , wherein the content of PB1 is 10-90 wt % and the content of PB2 is 0-60 wt % on a dry basis and based on the support , when characterizing PB1 by X-ray diffraction , κand κof said PB1 are respectively from more than 1 to less than or equal to 3 , wherein κ=h/h , κ=h/h , and h , hand hare respectively peak height of three diffraction peaks in the X-ray diffraction pattern of PB1 at 2θ angle of 24-30° , 35-41° and 46-52° , when characterizing PB2 by infrared spectrogram , δ value of PB2 is 1.5-4.5 , wherein δ=I/(I ...

Organosilica materials and uses thereof

Organosilica materials, which are a polymer of at least one independent monomer of Formula [Z 1 OZ 2 OSiCH 2 ] 3 (I), wherein each Z 1 and Z 2 independently represent a hydrogen atom, a C 1 -C 4 alkyl group or a bond to a silicon atom of another monomer and at least one other trivalent metal oxide monomer are provided herein. Methods of preparing and processes of using the organosilica materials, e.g., for catalysis etc., are also provided herein.

EPOXIDATION CATALYSTS BASED ON METAL ALKOXIDE PRETREATED SUPPORTS

The present disclosure generally relates to a silica-titanium catalyst prepared by first reacting a solid support with a metal alkoxide and then depositing titanium onto the solid support for the epoxidation of alkenes and aralkenes and a method of preparing the catalyst thereof. In some embodiments, the present disclosure relates to methods of using the catalyst described herein for the production of epoxides. 1. A method comprising:a) obtaining a solid silica support; {'br': None, 'sub': 'Y', 'SiX;'}, 'b) reacting the solid silica support with a silicon alkoxide of the formula [{'sub': (C≦12)', '(C≦12)', '(C≦12)', '(C≦12)', '(C≦12)', '(C≦12)', '(C≦12)', '(C≦12)', '(C≦12), 'each X is independently halide, alkoxylate, alkenyloxylate, alkynyloxylate, aryloxylate, heteroaryloxylate, aralkyloxylate, aralkenyloxylate, heterocycloalkyloxylate, acyloxylate, or a substituted version of any of these groups bearing a net negative charge; and'}, 'Y is equal to the oxidation state of Si; and, 'whereinc) depositing titanium from a titanium source on the solid silica support thereby forming a catalyst.2. The method of claim 1 , wherein the solid silica support has an average particle size of 0.7 mm-3.0 mm.3. The method of claim 1 , wherein the solid silica support has a surface area of 300-1100 m/g.4. The method of claim 1 , wherein the solid silica support has a pore volume of 0.5-3.0 mL/g.5. The method of claim 1 , wherein the silicon oxide has the formula:{'br': None, 'sub': '4', 'SiX;'} {'sub': (C≦12)', '(C≦12)', '(C≦12), 'each X is independently halide, alkoxylate, aralkoxylate, aryloxylate, or a substituted version of any of these groups.'}, 'wherein6. The method of claim 5 , wherein X is selected from the group consisting of methoxylate claim 5 , ethyoxylate claim 5 , isopropoxylate and tert-butoxylate.7. The method of claim 1 , wherein the titanium source is selected from the group consisting of titanium trihalide claim 1 , titanium tetrahalide and titanium ...

RESID HYDROTREATING CATALYST CONTAINING TITANIA

Improved catalyst supports, supported catalyst, and method of preparing and using the catalysts for the hydrodesulfurization of a residuum hydrocarbon feedstock are disclosed. The catalyst supports comprise titania alumina having 5 wt % or less titania and have greater than 70% of their pore volume in pores having a diameter between 70 Å and 130 Å and less than 2% in pores having a diameter above 1000 Å. Catalysts prepared from the supports contain Groups 6, 9 and 10 metals or metal compounds, and optionally phosphorus, supported on the titania alumina supports. Catalysts in accordance with the invention exhibit improved sulfur and MCR conversion in hydrotreating processes. 127-. (canceled)28. A process for preparing a porous support material for supporting catalytically active metals suitable for the hydrodesulfurization of residuum hydrocarbon fractions under hydrotreating conditions , which process comprises:a) preparing a co-precipitated titania alumina powder having 5 wt % or less titania, based on the total weight of the titania alumina powder; wherein the titania alumina is co-precipitated from an aqueous alumina and titanyl salt composition at a temperature of 63° C. to 80° C.;b) peptizing the titania alumina powder; (i) a total pore volume from about 0.5 to about 1.1 cubic centimeters per gramas determined by nitrogen porosimetry;', '(ii) at least 70% of the total pore volume in pores having a diameter of about 70 Å to about 130 Å as determined by nitrogen prosimetry;', '(iii) less than 5% of the total pore volume in pores having a diameter above 300 Å, as determined by nitrogen porosimetry, and', '(iv) less than 2% of the total pore volume in pores having a diameter above 1000 Å, as determined by mercury penetration porosimetry., 'c) extruding the titania alumina powder to form a titania alumina extrudate; and calcining the extrudate at a temperature from about 500° C. to about 900° C. for about 1 hour to about 3 hours to obtain a titania alumina support ...