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 ...

КАТАЛИЗАТОРЫ

Изобретение относится к предшественникам катализаторов Фишера-Тропша, содержащим носитель и кобальт на данном носителе, к катализаторам Фишера-Тропша, способу получения предшественников катализаторов и к применению карбоновой кислоты в указанном способе. Предшественник катализатора содержит (i) носитель катализатора, содержащий оксид кремния и 11-18% масс. TiO; и (ii) кобальт на данном носителе катализатора. Другой предшественник содержит (i) носитель катализатора, включающий оксид кремния и TiO; и (ii) 35-60% масс. Co, представленного как CoOна данном носителе катализатора, где среднечисловой диаметр частиц CoOсоставляет меньше чем 12 нм, определенный с помощью XRD, и С-величина логарифмически нормального распределения размера частиц CoOсоставляет от 0,19 до 0,31; или (b) D-величина логарифмически нормального распределения размера частиц составляет от 19 до 23,5. Способ получения предшественника катализатора включает следующие стадии: осаждают раствор или суспензию, содержащую, по меньшей ...

КАТАЛИЗАТОР И СПОСОБ РИФОРМИНГА КИСЛОРОДСОДЕРЖАЩИХ СОЕДИНЕНИЙ

Изобретение относится к области химии. Катализатор реформинга в водной фазе включает: а) углеродный носитель, включающий углерод, модифированный титаном, ванадием, вольфрамом или рением, и каталитическую композицию, прикрепленную к углеродному носителю. Каталитическая композиция включает Re и второй металл, выбранный из группы, состоящей из Ir, Ni, Pd, Pt, Rh и Ru, и Ce или La, прикрепленный к углеродному носителю или каталитической композиции. Для реформинга кислородсодержащих углеводородов приводят в контакт сырьевой раствор, включающий воду и по меньшей мере 20 мас.% в расчете на общую массу сырьевого раствора кислородсодержащего углеводорода с катализатором реформинга при условиях температуры реакции и давлении реакции, эффективных для получения газообразного водорода и алканов, имеющих от 1 до 8 атомов углерода. Кислородсодержащий углеводород имеет по меньшей мере один атом кислорода. Катализатор реформинга включает рений и по меньшей мере один переходный металл Группы VIII на водостойком ...

НОВЫЙ КОМПОЗИТНЫЙ МАТЕРИАЛ, СОДЕРЖАЩИЙ СОЕДИНЕНИЕ ЖЕЛЕЗА И ОКСИД ГРАФЕНА

Изобретение относится к химической промышленности и к нанотехнологии. Композитный материал с размером первичных частиц 0,1-100 мкм содержит оксид графена и 0,1-50 мас. % удерживаемого на нём соединения железа, например FeO, FeOили их смеси. Размер частиц соединения железа 0,1-10 нм. В инфракрасном спектре указанного композитного материала практически отсутствует поглощение, происходящее из O-H группы, поглощение, происходящее из C=O группы, и поглощение около 701 см, происходящее из Fe-O группы, но присутствует поглощение, происходящее из C-O группы. Для получения указанного композитного материала соответствующие сырьевые материалы суспендируют в инертном растворителе и облучают полученную суспензию УФ и видимым излучением с длиной волны 100-800 нм от 1 мин до 24 ч. В качестве сырьевого материала соединения железа используют по меньшей мере, один из: соли железа и неорганической кислоты, соли железа и карбоновой кислоты, соли железа и сульфоновой кислоты, гидроксида железа, фенольного железа ...

КАТАЛИТИЧЕСКИЙ НЕЙТРАЛИЗАТОР ДЛЯ ОЧИСТКИ ОТРАБОТАВШИХ ГАЗОВ С ОСЕВЫМ ВАРЬИРОВАНИЕМ КОНЦЕНТРАЦИИ ДРАГОЦЕННЫХ МЕТАЛЛОВ И СПОСОБЫ ИЗГОТОВЛЕНИЯ ЭТОГО КАТАЛИТИЧЕСКОГО НЕЙТРАЛИЗАТОРА

Изобретение относится к технологии очистки отработавших газов двигателей внутреннего сгорания. Каталитический нейтрализатор представляет собой сотовый элемент с входным и выходным концом и множеством проточных каналов, на который нанесено каталитическое покрытие. Каталитическое покрытие включает, по меньшей мере, один каталитически активный элемент из металлов платиновой группы, профиль концентрации которого непрерывно варьируется вдоль оси сотового элемента. Сотовый элемент разделен на три смежных участка. Концентрация активного элемента имеет низкое значение на первом участке, затем резко возрастает до пиковой на втором участке и уменьшается на третьем. Для изготовления нейтрализатора на сотовый элемент наносят материал с высокой удельной площадью поверхности. Затем отдельные участки смачивают смачивающим веществом, пропитывают соединением драгоценного металла, сушат и кальцинируют. Полученный каталитический нейтрализатор обладает повышенной стойкостью к отравлению и термическому разрушению ...

СПОСОБ ГИДРООЧИСТКИ ВАКУУМНОГО ДИСТИЛЛЯТА, ИСПОЛЬЗУЮЩИЙ ПОСЛЕДОВАТЕЛЬНОСТЬ КАТАЛИЗАТОРОВ

Изобретение относится к способу гидроочистки углеводородного сырья, содержащего соединения азота в количестве выше 250 в.ч./млн и имеющего средневзвешенную температуру кипения выше 380°С, включающему следующие стадии, на которых a) приводят в контакт в присутствии водорода указанное углеводородное сырье с по меньшей мере одним первым катализатором, включающим аморфную подложку на основе оксида алюминия, фосфор и активную фазу, образованную из по меньшей мере одного металла группы VIB в форме оксида и по меньшей мере одного металла группы VIII в форме оксида, причем указанный первый катализатор получен способом, включающим по меньшей мере один этап обжига, b) приводят в контакт в присутствии водорода поток, полученный на стадии а), с по меньшей мере одним вторым катализатором, включающим аморфную подложку на основе оксида алюминия, фосфор, активную фазу, образованную из по меньшей мере одного металла группы VIB и по меньшей мере одного металла группы VIII, и по меньшей мере одно органическое ...

Способ приготовления катализатора метатезиса низших олефинов, катализатор и его применение

Настоящее изобретение относится к методам получения катализаторов путем изменения кислотных свойств носителя активной фазы катализатора, к катализатору и применению катализатора для синтеза этилена или пропилена, включающему реакцию метатезиса олефинов, в которой в качестве исходного сырья используют смесь олефиновых углеводородов С2-С4. Способ получения оксидного катализатора включает обработку носителя, содержащего оксид алюминия, раствором соединений молибдена или вольфрама и последующее прокаливание до образования на носителе каталитически активной фазы в виде оксидов молибдена или вольфрама. В качестве алюмооксидного носителя берут оксид алюминия или алюминийсодержащий цеолит или глину. Носитель предварительно пропитывают по влагоёмкости модифицирующим раствором cолей, содержащих анионы, выбранные из ряда: F-, Cl-,Br-, I-,BF4-,SiF6-, SO42-, PO43-, BO33-. Пропитку осуществляют в течение времени, достаточного для замены поверхностных OH- групп носителя на анионы модифицирующих солей ...

СПОСОБ ИЗГОТОВЛЕНИЯ ЭЛЕКТРОКАТАЛИЗАТОРА ДЛЯ ТВЕРДОПОЛИМЕРНОГО ТОПЛИВНОГО ЭЛЕМЕНТА СО СТАБИЛИЗИРОВАННЫМ ВОДНЫМ БАЛАНСОМ

Изобретение относится к области технологии катализа и приготовления электрокатализаторов и может быть использовано в составе каталитического слоя мембранно-электродного блока (МЭБ) для топливного элемента с твердополимерным электролитом (ТЭ с ТПЭ). Предложен способ изготовления электрокатализатора для твердополимерного топливного элемента со стабилизированным водным балансом, заключающийся в том, что на исходный углеродный носитель наносят частицы SiO2 методом осаждения в объеме этиленгликоля для чего готовят суспензию, состоящую из носителя, смеси растворителей этиленгликоль - вода и изопропилового спирта, перемешивают суспензию с помощью ультразвуковой обработки, к полученной суспензии добавляют коллоидный раствор частиц кремнезема, и проводят осаждение, осуществляют синтез электрокатализатора на основе модифицированного носителя, для чего добавляют водный раствор гексахлорплатиновой кислоты и гомогенизируют его, полученный раствор по каплям приливают в емкость с модифицированным носителем ...

Гетерогенный катализатор жидкофазного окисления органических соединений и способ его получения

Изобретение относится к химической промышленности, а именно к области производства гетерогенных катализаторов процессов жидкофазного окисления органических соединений (в том числе производных фенолов), и может быть применено на предприятиях различных отраслей промышленности для проведения реакций окисления, а также для каталитической очистки сточных вод от токсичных органических загрязнителей. Гетерогенный катализатор жидкофазного окисления органических соединений содержит носитель, модифицированный 3-аминопропилтриэтоксисиланом, глутаровый диальдегид в качестве сшивающего агента и пероксидазу корня хрена в качестве активного компонента, в котором носителем являются магнитные наночастицы Fe3O4, модифицированные SiO2, при следующем соотношении компонентов, % мас.: Fe3O4- 34,2÷34,6; SiO2- 41,0÷41,4; 3-аминопропилтриэтоксисилан - 18,3÷18,8; глутаровый диальдегид - 3,8÷4,0; пероксидаза хрена - 1,9÷2,0. Способ получения гетерогенного катализатора жидкофазного окисления органических соединений ...

СПОСОБ ИЗГОТОВЛЕНИЯ КАТАЛИЗАТОРА НА МЕТАЛЛИЧЕСКОЙ ПОДЛОЖКЕ

... 1. Способ изготовления катализатора на металлической подложке, включающий: ! связывание соединения, содержащего координируемую функциональную группу с подложкой катализатора; ! пропитку подложки катализатора, с которой связано соединение, раствором, который содержит металлический комплекс, в котором лиганд координирован одним атомом металла катализатора или множеством атомов металла катализатора того же самого вида, и замещение, по меньшей мере, частично, лиганда, координированного металлическим комплексом, координируемой функциональной группой соединения; и ! высушивание и обжигание подложки катализатора, пропитанной раствором. ! 2. Способ изготовления катализатора на металлической подложке по п.1, в котором металлическим комплексом является многоядерный комплекс. ! 3. Способ изготовления катализатора на металлической подложке по п.1 или 2, в котором соединение, связанное с подложкой катализатора имеет множество координируемых функциональных групп. ! 4. Способ изготовления катализатора ...

КАТАЛИЗАТОРЫ

Предложен способ получения предшественника катализатора. Способ получения предшественника катализатора включает: получение суспензии, включающей жидкость-носитель, растворимую соль металла, частицы нерастворимой неорганической соли металла и частицы и/или одно или более тел предварительно сформованных носителей катализатора, с осаждением металла из нерастворимой соли металла на частицах носителя за счет хемосорбции, и с осаждением металла из растворимой соли металла внутри и/или на частицах носителя за счет пропитки, при этом хемосорбция и пропитка осуществляются одновременно, и металлы в нерастворимой неорганической соли металла и в растворимой соли металла являются одними и теми же, и представляют собой Со или Ni, и при этом указанный металл является активным компонентом катализатора, с образованием обработанного носителя катализатора, и удаление жидкости-носителя из суспензии с получением высушенного обработанного носителя катализатора, который или непосредственно представляет собой ...

КАТАЛИЗАТОРЫ, СОДЕРЖАЩИЕ БЛАГОРОДНЫЙ МЕТАЛЛ И ЛАНТАНИД, НАНЕСЕННЫЕ НА ПО СУЩЕСТВУ НЕПОРИСТУЮ ПОДЛОЖКУ

Изобретение относится к катализатору для использования в процессах гидрирования. Предлагаемый катализатор содержит благородный металл, который представляет собой палладий, и элемент группы лантанидов, который представляет собой европий, нанесенные на носитель, содержащий по существу непористую стеклосодержащую подложку. Данная стеклосодержащая подложка имеет удельную поверхность, измеренную методом S.A., основанном на тепловой адсорбции/десорбции N, или методом S.A., основанном на тепловой адсорбции/десорбции Kr, в диапазоне от 0,01 м/г до 10 м/г, и скорость изменения удельной поверхности по хемосорбции натрия SACR≤0,5. При этом палладий и европий каждый присутствуют в количестве от 10 частей на миллион по весу до 1% по весу, исходя из веса катализатора. Предлагаемый катализатор обладает селективностью и стабильностью в активности в процессах гидрирования. Изобретение также относится к способу гидрирования сырьевого потока в присутствии данного катализатора и способу получения такого катализатора ...

КОМПЛЕКС СОЕДИНЕНИЯ МЕТАЛЛА - ОКСИДА ГРАФЕНА

КАТАЛИЗАТОР ОКИСЛЕНИЯ, СОДЕРЖАЩИЙ СОЕДИНЕНИЕ СЕРЫ

КАТАЛИЗАТОР ГИДРООЧИСТКИ С ТИТАНСОДЕРЖАЩИМ НОСИТЕЛЕМ И СЕРОСОДЕРЖАЩЕЙ ОРГАНИЧЕСКОЙ ДОБАВКОЙ

СПОСОБ ПОЛУЧЕНИЯ НЕНАСЫЩЕННОГО УГЛЕВОДОРОДА

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

КАТАЛИЗАТОРЫ И СПОСОБЫ РЕФОРМИНГА КИСЛОРОДСОДЕРЖАЩИХ СОЕДИНЕНИЙ

... 1. Способ реформинга кислородсодержащих углеводородов, включающий стадию приведения в контакт сырьевого раствора, включающего воду и по меньшей мере 20 мас.%, в расчете на общую массу сырьевого раствора, кислородсодержащего углеводорода, с катализатором реформинга при условиях температуры реакции и давления реакции, эффективных для получения газообразного водорода и алканов, имеющих от 1 до 8 атомов углерода, где кислородсодержащий углеводород имеет по меньшей мере один атом кислорода и где катализатор реформинга включает рений и по меньшей мере один переходный металл группы VIII на водостойком носителе. ! 2. Способ по п.1, где конверсия в газообразный водород больше с катализатором реформинга, чем конверсия в газообразный водород при использовании аналогичного сырьевого раствора и аналогичного катализатора с отсутствием рения. ! 3. Способ по п.1, где конверсия в алканы с катализатором реформинга больше, чем конверсия в алканы при использовании аналогичного сырьевого раствора и аналогичного ...

СПОСОБ ПОЛУЧЕНИЯ ПОЛИМЕТАЛЛИЧЕСКОГО КАТАЛИЗАТОРА С ОПТИМИЗИРОВАННОЙ БЛИЗОСТЬЮ ЦЕНТРОВ

... 1. Способ получения катализатора, содержащего по меньшей мере один металл М из группы платины, олово, фосфорный промотор, галогенсодержащее соединение, пористую подложку и по меньшей мере один промотор X1, выбранный из группы, состоящей из галлия, индия, таллия, мышьяка, сурьмы и висмута, причем указанный способ включает следующие этапы:a) введение промотора или промоторов X1 и фосфора на подэтапе или подэтапах а1) или а2), причем указанный подэтап а1) соответствует синтезу предшественника основного оксида, а указанный подэтап а2) соответствует формованию подложки,b) введение олова на по меньшей мере одном из подэтапов а1) и а2), причем этапы а) и b) могут быть последовательными или одновременными,c) сушку продукта, полученного на выходе с этапа b),d) обжиг продукта, полученного на этапе с), при температуре от 350°С до 650°С,e) осаждение по меньшей мере одного металла М группы платины,f) сушку в потоке нейтрального газа или в потоке газа, содержащего кислород, при умеренной температуре, ...

ПОЛИМЕТАЛЛИЧЕСКИЙ КАТАЛИЗАТОР С СИЛЬНЫМ МЕЖМЕТАЛЛИЧЕСКИМ ВЗАИМОДЕЙСТВИЕМ

... 1. Катализатор, содержащий по меньшей мере один металл M группы платины, олово, фосфорный промотор, галогенсодержащее соединение, пористую подложку и по меньшей мере один промотор X1, выбранный из группы, состоящей из галлия, индия, таллия, мышьяка, сурьмы и висмута, причем указанный катализатор в восстановленной форме демонстрирует, согласно мессбауэровской спектроскопииSn, сигнал, имеющий величину квадрупольного расщепления от 0 до 0,45 мм/с и химический сдвиг IS от 1,5 до 2,4 мм/с относительно CaSnO, причем площадь указанного сигнала составляет от 1% до 30% общей площади сигналов.2. Катализатор по п.1, в котором атомное отношение Sn/M составляет от 0,5 до 4,0.3. Катализатор по п.1, в котором отношение X1/M составляет от 0,1 до 5,0.4. Катализатор по п.1, в котором отношение P/M составляет от 0,2 до 30,0.5. Катализатор по одному из пп.1-4, в котором содержание металла M составляет от 0,01 до 5 вес.%.6. Катализатор по п.5, в котором металл M является платиной или палладием.7. Катализатор ...

КАТАЛИЗАТОР СИНТЕЗА ЭТИЛЕНОКСИДА

... 1. Способ приготовления катализатора синтеза этиленоксида, представляющего собой серебро на носителе из оксида алюминия, который включает контактирование алюминий-оксидного носителя с водным основным раствором при температуре ниже 100°С и поддержание рН основного раствора выше 8 во время обработки путем добавления основания. 2. Способ по п.1, в котором рН поддерживают выше 9. 3. Способ по п.1, в котором рН поддерживают в интервале 10-13. 4. Способ по п.1, в котором основание добавляют к водному раствору соли во время обработки носителя.

СПОСОБ ПОЛУЧЕНИЯ ГИДРОТЕРМАЛЬНО СТАБИЛЬНЫХ КАТАЛИЗАТОРОВ КОНВЕРСИИ СИНТЕЗ-ГАЗА В УГЛЕВОДОРОДЫ, СПОСОБ ПОЛУЧЕНИЯ УГЛЕВОДОРОДОВ И КАТАЛИЗАТОР С ПОВЫШЕННОЙ ГИДРОТЕРМАЛЬНОЙ СТАБИЛЬНОСТЬЮ

... 1. Способ получения гидротермально стабильных катализаторов конверсии синтез-газа в углеводороды, отличающийся тем, что наносят по крайней мере одно соединение каталитического металла, выбранного из металлов 8, 9 и 10 групп Периодической таблицы, на материал носителя, включающий бемит, с образованием композиционного материала; и прокаливают полученный композиционный материал. 2. Способ по п.1, отличающийся тем, что бемит представляет собой синтетический бемит, природный бемит, псевдобемит или их комбинации. 3. Способ по п.1, отличающийся тем, что бемит содержится в виде частиц, причем частицы характеризуются размером в интервале от приблизительно 20 мкм до приблизительно 200 мкм. 4. Способ по п.1, отличающийся тем, что бемит содержится в виде частиц, причем частицы характеризуются средним размером в диапазоне от приблизительно 50 мкм до приблизительно 90 мкм. 5. Способ по п.1, отличающийся тем, что дополнительно производят предварительный нагрев материала носителя при температуре в интервале ...

КАТАЛИЗАТОРЫ НА ОСНОВЕ КОБАЛЬТА

... 1. Способ получения предшественника катализатора на основе кобальта, включающий пропитку пористых частиц носителя для катализатора солью кобальта, частичную сушку пропитанного носителя и прокаливание частично высушенного пропитанного носителя с получением прокаленного продукта, содержащего исходную окись кобальта; частичное восстановление прокаленного продукта с тем, чтобы исходная окись кобальта частично восстановилась до СоО, с получением частично восстановленного продукта, и пропитку частично восстановленного продукта солью кобальта, частичную сушку пропитанного продукта и прокаливание частично высушенного пропитанного продукта с получением предшественника катализатора на основе кобальта. 2. Способ получения катализатора Фишера-Тропша на основе кобальта, включающий пропитку пористых частиц носителя для катализатора солью кобальта, частичную сушку пропитанного носителя и прокаливание частично высушенного пропитанного носителя с получением прокаленного продукта, содержащего исходную окись ...

VERFAHREN UND KATALYSATOR ZUM REFORMIEREN VON KOHLENWASSERSTOFFEN SOWIE VERFAHREN ZUM HERSTELLEN DES KATALYSATORS

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 ...

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

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

Katalysator und Verfahren zur Reinigung von Abgasen

Verfahren zum Vorbereiten eines Mehrkomponenten-Legierungskatalysators

Ein Verfahren zum Vorbereiten eines Mehrkomponenten-Legierungskatalysators, auf dem ein katalytisches Metall getragen wird, enthält das Vorbereiten eines Kohlenstoffverbundstoffes, der einen Kohlenstoffträger aufweist, der mit einem kationischen Polymer beschichtet ist, Tragen eines katalytischen Metalls, das zumindest zwei Metallelemente enthält, auf dem Kohlenstoffverbundstoff, um einen Legierungskatalysator-Vorläufer vorzubereiten, und Waschen des Legierungskatalysator-Vorläufers, um das kationische Polymer zu entfernen.

Treating of catalyst carrier, fischer - trpsch catalysts and method of preparation thereof

Three-way catalyst and its use in exhaust systems

A selective nickle based hydrogenation catalyst and the preparation thereof

Treating of catalyst carrier, fischer - tropsch catalysts and method of preparation thereof

A method for the preparation of a modified catalyst support comprising: (a) treating a bare catalyst support material with an aqueous solution or dispersion of one or more titanium metal sources and one or more carboxylic acids; and (b) drying the treated support, and (c) optionally calcining the treated support. Also provided are catalyst support materials obtainable by the methods, and catalysts prepared from such supports. The method of preparation improves the stability of the modified catalyst support. The catalyst prepared with the treated support are also more active compare with catalyst having a support, which is not prepared according to the method of the application.

Selective catalytic reduction catalyst composition

A selective catalytic reduction catalyst (SCR) composition comprises a SCR catalyst; and a binder comprising a porous inorganic material which comprises a disordered arrangement of delaminated layers, has a disordered porous structure, and a multimodal pore size distribution comprising at least a first modal maximum having a macroporous or mesoporous pore size and a second modal maximum having a microporous pore size. The catalyst may be an Fe or Cu SCR, and the porous inorganic material may be a clay such as a three layered (2:1) clay mineral, e.g. bentonite. The catalyst composition is manufactured using a method comprising the steps of: (I) providing an inorganic material having a layered structure; (ii) contacting the material with a cationic surfactant to form a swollen material; (iii) agitating the swollen material to form an agitated material; and (iv) calcining the agitated material to recover a delaminated inorganic material, wherein an SCR catalyst is mixed with the inorganic ...

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

Fischer-tropsch synthesis

Catalysts

Process for preparing a cobalt-containing hydrocarbon synthesis catalyst precursor

Production of hydrocarbons.

Fischer-tropsch process in a microchannel reactor

PROCESS FOR PREPARING A COBALT - CONTAINING HYDROCARBON SYNTHESIS CATALYST PRECURSOR

Production of hydrocarbons

Catalyst supports made from silicon carbide with TIO2 for Fischer-Tropsch synthesis

Catalysts

Fischer-tropsch process in a microchannel reactor

Process for preparing a cobalt-containing hydrocarbon synthesis catalyst precursor

Process for preparing a cobalt-containing hydrocarbon synthesis catalyst precursor

Catalyst

A process for preparing a cobalt-containing hydrocarbon synthesis catalyst precursor

Highly active fischer-tropsch synthesis using doped, thermally stable catalyst support.

Reducing fischer-tropsch catalyst attrition lossesin high agitation reaction systems.

Improved fischer-tropsch activity for non-promotedcobalt-on-alumina catalysts.

Catalyst

Catalyst supports made from silicon carbide with TIO2 for Fischer-Tropsch synthesis

Fischer-tropsch process in a microchannel reactor

Production of hydrocarbons.

Catalyst

A process for preparing a cobalt-containing hydrocarbon synthesis catalyst precursor

Catalysts

Production of hydrocarbons.

Fischer-tropsch process in a microchannel reactor

A process for preparing a cobalt-containing hydrocarbon synthesis catalyst precursor

PROCEDURE FOR TREATING FLUE GAS CATALYSTS

ISOLATING ONE AND FUNCTIONAL ONE FINE METALLIFEROUS PARTICLES WITH CONFORMAL ULTRADÜNNEN FILMS

COOXIDATIONSPROMOTOREN FOR USE WITH FCC PROCEDURES

PROCEDURE FOR THE PRODUCTION OF CARRIER CATALYSTS FROM METAL-LOADED CARBON NANO-TUBES

PROCEDURE FOR REFORMING A KOHL HYDROGEN

IMPROVED CATALYSTS FOR the HYDROGENATION FROM MALEIC ACID TO 1,4-BUTANDIOL

BISMUTH AND PHOSPHORUS OF CONTAINING KATALYSATORTRÄGER, WITH THIS CARRIER OF MANUFACTURE REFORMATION CATALYST AS WELL AS ITS MANUFACTURING PROCESSES AND USE WHEN REFORMING NAPHTA

CATALYTIC HYDRAULIC REFORMATION PROCEDURES

PROCEDURE FOR THE PRODUCTION OF FISCHER TROPSCH CATALYSTS

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

The invention provides a process for preparing a methane oxidation catalyst, a methane oxidation catalyst thus prepared and a method of oxidizing methane.

Stabilized boehmite-derived catalyst supports, catalysts, methods of making and using

Fast activating catalyst

Fischer-Tropsch catalysts

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

Ethylene oxide catalyst

Cobalt catalysts

BISMUTH-AND PHOSPHORUS-CONTAINING CATALYSTS SUPPORT, REFORMING CATALYSTS MADE FROM SAME, METHOD OF MAKING AND NAPHTHA REFORMING PROCESS

Production of liquid hydrocarbons

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

Production of hydrocarbons

A process for producing hydrocarbons and, optionally, oxygenates of hydrocarbons is provided. A synthesis gas comprises hydrogen, carbon monoxide and N-containing contaminants selected from the group consisting of HCN, NH, NO, RNH, R-CN and heterocyclic compounds containing at least one nitrogen atom as a ring member of a heterocyclic ring of the heterocyclic compound. The N-containing contaminants constitute, in total, at least 100vppb but less than 1 000 000vppb of the synthesis gas. The synthesis gas is contacted at an elevated temperature and an elevated pressure, with a particulate supported Fischer-Tropsch synthesis catalyst. The catalyst comprises a catalyst support, Co in catalytically active form supported on the catalyst support, and a dopant selected from the group consisting of platinum (Pt), palladium (Pd), ruthenium (Ru) and/or rhenium (Re). The dopant level is expressed by a formula. Hydrocarbons and, optionally, oxygenates of hydrocarbons are obtained.

COBALT CATALYST

Layered catalyst composition and processes for preparing and using the composition

Supported catalyst consisting of metal of the platinum group and obtained by means of controlled electroless deposition

STABILIZED BOEHMITE-DERIVED CATALYST SUPPORTS, CATALYSTS, METHODS OF MAKING AND USING

A stabilized catalyst support having improved hydrothermal stability, catalyst made therefrom, and method for producing hydrocarbons from synthesis gas using said catalyst. The stabilized support is made by a method comprising treating a crystalline hydrous alumina precursor in contact with at least one structural stabilizer or compound thereof. The crystalline hydrous alumina precursor preferably includes an average crystallite size selected from an optimum range delimited by desired hydrothermal resistance and desired porosity. The crystalline hydrous alumina precursor preferably includes an alumina hydroxide, such as crystalline boehmite, crystalline bayerite, or a plurality thereof differing in average crystallite sizes by at least about 1 nm. The crystalline hydrous alumina precursor may be shaped before or after contact with the structural stabilizer or compound thereof. The treating includes calcining at 450oC or more. Preferred structural stabilizers can include cobalt, magnesium ...

NON-ZEOLITIC NANOCOMPOSITE MATERIALS FOR SOLID ACID CATALYSIS

One aspect of the present invention relates to a catalytic compound of anion- modified metal oxides doped with metal ions. Another aspect of the present invention relates to a method of isomerizing an alkane or alkyl moiety.

CATALYSTS FOR MAKING ETHANOL FROM ACETIC ACID

Catalysts and processes for forming catalysts for use in hydrogenating acetic acid to form ethanol. In one embodiment, the catalyst comprises a first metal, a silicaceous support, and at least one metasilicate support modifier. Preferably, the first metal is selected from the group consisting of copper, iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, platinum, titanium, zinc, chromium, rhenium, molybdenum, and tungsten. In addition the catalyst may comprise a second metal preferably selected from the group consisting of copper, molybdenum, tin, chromium, iron, cobalt, vanadium, tungsten, palladium, platinum, lanthanum, cerium, manganese, ruthenium, rhenium, gold, and nickel.

A TRANSPARENT PHOTOCATALYTIC COATING FOR IN-SITU GENERATION OF FREE RADICALS COMBATING MICROBES, ODORS OR ORGANIC COMPOUNDS IN VISIBLE LIGHT

A transparent photocatalytic coating for in-situ generation of free radicals combating microbes, odors and organic compounds in visible light is disclosed, featuring a catalytic material comprising a dopant and having particle size distribution suitable for exciton-confinment to accumulatively shift the photocatalytic process into visible light range. Furthermore, the present invention features a method of producing the photocatalytic material described herein. Furthermore, the present invention discloses a method of application of the photocatalytic coating to a surface of a locus. Finally, the present invention features using the photocatalytic coating for removing contaminants and microorganisms at the locus.

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

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

REFORMING CATALYST

A reforming catalyst comprising precious metal particles dispersed on a support material, wherein the support material comprises ceria, and characterised in that the support material further comprises magnesium aluminate is disclosed. Catalysed components and fuel processing systems comprising the catalyst, and reforming processes using the catalyst are also disclosed.

ETHYLENE OXIDE CATALYST

ON-LINE SYNTHESIS AND REGENERATION OF A CATALYST USED IN AUTOTHERMAL OXIDATION

An on-line method of synthesizing or regenerating catalysts for autothermal oxidation processes, specifically, the oxidation of paraffinic hydrocarbons, for example, ethane, propane, and naphtha, to olefins, for example, ethylene and propylene. The catalyst comprises a Group 8B metal, for example, a platinum group metal and, optionally, a promoter, such as tin, antimony, or copper, on a support, preferably a monolith support. On-line synthesis or regeneration involves co-feeding a volatile Group 8B metal compound and/or a volatile promoter compound with the paraffinic hydrocarbon and oxygen into the oxidation reactor under ignition or autothermal conditions.

PROCESS FOR CONVERTING SYNTHESIS GAS IN THE PRESENCE OF A CATALYST HAVING A GROUP VIII ELEMENT DISPERSED ON A ALUMIN-BASED MEDIUM MODIFIED BY AQUEOUS IMPREGNATION OF QUATERNARY AMMONIUM SILICATE

Procédé de conversion du gaz de synthèse en présence d'un catalyseur comprenant au moins un élément du groupe VIII dispersé sur un support comprenant de l'alumine modifiée par imprégnation aqueuse de silicate d'ammonium quaternaire et comprenant entre environ 3 %poids et environ 9,5 %poids de silice. Ledit support peut éventuellement comprendre en outre au moins un oxyde choisi dans le groupe constitué par les oxydes de terre rare, les oxydes d'alcalino-terreux et l'oxyde de zirconium.

CATALYST FOR PURIFICATION OF EXHAUST GAS, REGENERATION METHOD FOR THE CATALYST, AND APPARATUS AND METHOD FOR PURIFICATION OF EXHAUST GAS USING THE CATALYST

A catalyst for purification of exhaust gas in which a noble metal is supported on a metal-oxide support wherein, in a oxidation atmosphere, the noble metal exists on the surface of the support in high oxidation state, and the noble metal binds with a cation of the support via an oxygen atom on the surface of the support to form a surface oxide layer and, in a reduction atmosphere, the noble metal exists on the surface of the support in a metal state, and an amount of noble metal exposed at the surface of the support, measured by Co chemisorption, is 10% or more in atomic ratio to a whole amount of the noble metal supported on the support.

REFORMING CATALYST AND A METHOD OF PREPARATION THEREOF

The present disclosure relates to a reforming catalyst composition comprising a spherical gamma AI2O3 support; at least one Group VB metal oxide sheet coated on to the AI2O3 support; and at least one active metal and at least one promoter metal impregnated on the AI2O3 coated support. The reforming catalyst composition of the present disclosure has improved activity, better selectivity for total aromatics during naphtha reforming and results in less coke formation. The reforming catalyst composition has improved catalyst performance with simultaneous modification of acidic sites as well as metallic sites through metal support interaction. The acid site cracking activity of the catalyst is inhibited because of the use of chloride free alumina support modified with solid acid such as Group VB metal oxide and impregnated with active metals. The present disclosure provides a process for naphtha reforming in the presence of the reforming catalyst composition of the present disclosure to obtain ...

CATALYST FOR THE SYNTHESIS OF METHYL MERCAPTAN AND PROCESS FOR PRODUCING METHYL MERCAPTAN FROM SYNTHESIS GAS AND HYDROGEN SULPHIDE

L 'invention porte sur un catalyseur comprenant un composant actif à base de molybdène et de potassium et un support à base d' hydroxyapatite, ainsi que sur un procédé de préparation dudit catalyseur et un procédé de production de méthyl mercaptan dans un procédé catalytique par réaction d' oxyde de carbone, de soufre et/ou de sulfure d'hydrogène et d 'hydrogène, comprenant l 'utilisation dudit catalyseur.

Method for Producing Ethanol

A method for producing ethanol by which ethanol can be synthesized from less fermentable biomass materials such as plant-derived materials and rice straws and industrial waste biomass materials such as wooden building materials and pulp and which can therefore broaden the range of raw materials for the production of ethanol. Specifically, a method for producing ethanol including reacting a raw material gas obtained by a thermochemical gasification reaction of biomass in the presence of a catalyst containing rhodium, at least one transition metal, and at least one element selected from lithium, magnesium and zinc.

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

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

Method for preparing a multi-metal catalyst having an optimized site proximity

The invention concerns a process for preparing a catalyst comprising at least one metal M from the platinum group, tin, a phosphorus promoter, a halogenated compound, a porous support and at least one promoter X1 selected from the group constituted by gallium, indium, thallium, arsenic, antimony and bismuth. The promoter or promoters X1 and the phosphorus are introduced during one or more sub-steps a1) or a2), the sub-step a1) corresponding to synthesis of the precursor of the main oxide and sub-step a2) corresponding to shaping the support. The tin is introduced during at least one of sub-steps a1) and a2). The product is dried and calcined before depositing at least one metal M from the platinum group. The ensemble is then dried in a stream of neutral gas or a stream of gas containing oxygen, and then is dried. The invention also concerns the use of a catalyst obtained by said process in catalytic reforming or aromatics production reactions.

Production of hydrocarbons

A process for producing hydrocarbons and, optionally, oxygenates of hydrocarbons is provided. A synthesis gas comprises hydrogen, carbon monoxide and N-containing contaminants selected from the group consisting of HCN, NH 3 , NO, R X NH 3-X , R 1 —CN and heterocyclic compounds containing at least one nitrogen atom as a ring member of a heterocyclic ring of the heterocyclic compound. The N-containing contaminants constitute, in total, at least 100 vppb but less than 1 000 000 vppb of the synthesis gas. The synthesis gas is contacted at an elevated temperature and an elevated pressure, with a particulate supported Fischer-Tropsch synthesis catalyst. The catalyst comprises a catalyst support, Co in catalytically active form supported on the catalyst support, and a dopant selected from the group consisting of platinum (Pt), palladium (Pd), ruthenium (Ru) and/or rhenium (Re). The dopant level is expressed by a formula. Hydrocarbons and, optionally, oxygenates of hydrocarbons are obtained.

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

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

Method for Producing 3,3,3-Trifluoro Propene

A production method of 3,3,3-trifluoropropene includes the step of hydrogenating 1-chloro-3,3,3-trifluoropropene with hydrogen (H 2 ) in a gas phase in the presence of either of: (A) a catalyst having carried on a carrier at least one kind of transition metal selected from the group consisting of ruthenium, nickel, rhodium, iridium, iron, osmium and cobalt, or an oxide of said transition metal; (B) an oxide catalyst of copper and manganese; and (C) a catalyst having carried on a carrier palladium and at least one kind of element selected from the group consisting of bismuth, zinc, copper, silver, lanthanum, lead, zirconium, niobium, hafnium, magnesium, tin and arsenic.

Catalyst treatment

A method of preparing a Fischer-Tropsch catalyst for handling, storage, transport and deployment, including the steps of impregnating a porous support material with a source of cobalt, calcining the impregnated support material activating the catalyst, and passivating the activated catalyst.

Process for the preparation of a catalyst support

Process for preparing a catalyst support which process comprises a) mixing pentasil zeolite having a bulk silica to alumina molar ratio in the range of from 20 to 150 with water, a silica source and an alkali metal salt, b) extruding the mixture obtained in step (a), c) drying and calcining the extrudates obtained in step (b), d) subjecting the calcined extrudates obtained in step (c) to ion exchange to reduce the alkali metal content, and e) drying the extrudates obtained in step (d); process for preparing a catalyst by furthermore impregnating such support with platinum in an amount in the range of from 0.001 to 0.1 wt % and tin in an amount in the range of from 0.01 to 0.5 wt %, each on the basis of total catalyst; ethylbenzene dealkylation catalyst obtainable thereby and a process for dealkylation of ethylbenzene which process comprises contacting feedstock containing ethylbenzene with such catalyst.

Catalyst and method for the production of chlorine by gas phase oxidation

The present invention relates to a catalyst for preparation of chlorine by catalytic gas phase oxidation of hydrogen chloride with oxygen, in which the catalyst comprises calcined tin dioxide as a support and at least one halogen-containing ruthenium compound, and to the use thereof.

Catalyst support materials with oxygen storage capacity (osc) and method of making thereof

A new type of catalyst support with oxygen storage capacity (OSC) and methods of making the same are disclosed. The composition ratio is x(Ce 1-w Zr w 0 2 ):yM:zL:(1-x-y-z)AI 2 0 3 , where Ce 1-w Zr w 0 2 is the oxygen storage composition with stabilizer Zr0 2 , molar ratio (w) in the range of 0 to about 0.8, and a weight ratio (x) of about 0.05 to about 0.8; M is an interactive promoter for oxygen storage capacity with a weight ratio (y) of 0 to about 0.10; and L is a stabilizer for the support Al 2 0 3 with weight ratio (z) of from 0 to about 0.10. In some cases, M or L can act as both OSC promoter and thermal stabilizer. The weight percentage range of ceria-zirconia and other metal and rare earth oxides (x+y+z) is from about 5 to about 80% relative to total oxides. Combining platinum group metals (PGM) and adhesive with the catalyst supports, a new wash coat made therefrom is provided that comprises a mixture of catalyst support materials according to the relationship (a)RE-Ce—Zr0 2 +(3)CZMLA+(1-a-β)RE-AI 2 0 3 , where RE-Ce—Zr0 2 is a commercial OSC material of rare earth elements stabilized ceria zirconia having a weight ratio (a) ranging from 0 to about 0.7; CZMLA is the catalyst support material of the present disclosure having a weight ratio (β) ranging from about 0.2 to about 1 such that (α+β)<1; and RE-AI 2 0 3 is rare earth element stabilized alumina having a weight ratio equal to (1-α-β). The new wash coat made therefrom exhibits a lower activation temperature compared with traditional formulation of wash coat by at least 50° C. The new wash coat made therefrom also requires less RE-Ce—Zr0 2 oxide and/or less PGM in the formulation of emission control catalyst for gasoline and diesel engines.

Capture mass composed of elemental sulphur deposited on a porous support for capturing heavy metals

The present invention concerns the elimination of heavy metals, in particular mercury and possibly arsenic and lead, present in a dry or moist gaseous effluent ( 1 ) by means of a capture mass ( 2 ) comprising a porous support at least part of which is of low mesoporosity and an active phase based on sulphur. The invention is advantageously applicable to the treatment of gas of industrial origin, synthesis gas or natural gas.

Process for pre-treatment of a catalyst support and catalyst prepared therefrom

Methods of forming noble metal catalysts, noble metal catalysts formed therefrom and process for using noble metal catalysts are described herein. The methods generally include contacting a support material with a pre-treatment agent including a dilute basic solution of an alkali or alkaline earth metal to form a contacted support; drying the contacted support to form a pre-treated support; and impregnating the pre-treated support with at least one noble metal to form the noble metal catalyst.

METHODS FOR PRODUCING MESOPOROUS ZEOLITE MULTIFUNCTIONAL CATALYSTS FOR UPGRADING PYROLYSIS OIL

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

METHODS FOR PRODUCING MULTIFUNCTIONAL CATALYSTS FOR UPGRADING PYROLYSIS OIL

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

METHODS FOR PRODUCING MULTIFUNCTIONAL CATALYSTS FOR UPGRADING PYROLYSIS OIL

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

Method For Producing Hydrocarbon Dehydrogenation Catalyst Using Sponge-Type Support

Disclosed are a catalyst for dehydrogenating a paraffinic hydrocarbon and a method of preparing the same, wherein the catalyst is configured such that a sponge-type alumina support having 3D meso/macro pores is directly impregnated with an active metal, thus decreasing the diffusion resistance of a material, realizing structural stability, and maximizing the distribution of the active metal in the support, thereby significantly increasing olefin conversion and selectivity. 1. A method of preparing a catalyst for dehydrogenating paraffin , comprising:providing a sponge-type alumina support having meso/macro pore sizes;thermally treating the support at 800 to 1200° C. for 2 to 10 hr in an air atmosphere;dispersing an active metal precursor in the support so as to be loaded into the support;drying the support having the loaded active metal at 80 to 150° C.; andfiring the dried catalyst at 500 to 900° C. for 2 to 10 hr in an air atmosphere.2. The method of claim 1 , further comprising reducing the fired catalyst at 400 to 700° C. in a hydrogen atmosphere claim 1 , after the firing the dried catalyst.3. The method of claim 1 , wherein the active metal comprises platinum claim 1 , tin claim 1 , or an alkali metal or alkaline earth metal.4. The method of claim 1 , wherein the sponge-type alumina support comprises two kinds of pores having a meso pore size and a macro pore size.5. The method of claim 1 , wherein the sponge-type alumina support is selected from the group consisting of alpha alumina claim 1 , theta alumina claim 1 , silicon carbide claim 1 , and mixtures thereof.6. The method of claim 1 , wherein the sponge-type alumina support has a specific surface area of 50 to 100 m/g claim 1 , a total pore volume of 0.1 to 0.7 cm/g claim 1 , and a pore size of 10 to 100 nm.7. A catalyst for dehydrogenating paraffin claim 1 , prepared by the method of any one of to .8. A method of producing an olefin claim 7 , comprising dehydrogenating a gas mixture comprising paraffin ...

Palladium Catalysts Supported on Carbon for Hydrogenation of Aromatic Hydrocarbons

Provided is a process for preparing partially or fully hydrogenated hydrocarbons through hydrogenation of aromatic hydrocarbons in the presence of a hydrogenation catalyst. The hydrogenation catalyst comprises palladium deposited on carbon with optional acid wash and calcination treatments and with optional additions of silver and/or alkali metals. 1. A chemical catalyst , comprising an acid-washed carbon base and palladium deposited on said carbon base.2. The chemical catalyst of claim 1 , wherein said carbon base is an activated carbon base.3. The chemical catalyst of claim 1 , wherein said carbon base is calcinated before said palladium is deposited thereon.4. The chemical catalyst of claim 1 , wherein said catalyst comprises from about 0.1 to about 5 weight percentage of palladium.5. The chemical catalyst of claim 1 , further comprising a metal additive deposited on said carbon base with said palladium.6. The chemical catalyst of claim 5 , wherein the molar ratio of said palladium to said metal additive is in a range of from 1:1 to 12:1.7. The chemical catalyst of claim 5 , wherein said metal additive comprises a metal selected from the group consisting of alkali metals and silver.8. A method of making a chemical catalyst claim 5 , comprising the steps of:(i) dissolving a first precursor in deionized water to form a solution;(ii) depositing said solution onto an acid-washed carbon base; and(iii) drying said carbon base in the presence of static air.9. The method of claim 8 , wherein step (ii) is conducted according to the incipient wetness method.10. The method of claim 8 , wherein said carbon base is an activated carbon base.11. The method of claim 8 , further comprising the step of calcining said carbon base prior to the performance of step (ii).12. The method of claim 11 , wherein no calcination treatment is applied to said carbon base following the performance of step (ii).13. The method of claim 11 , wherein said calcining step involves subjecting said ...

GOLD-BASED CATALYST FOR THE OXIDATIVE ESTERIFICATION OF ALDEHYDES TO OBTAIN CARBOXYLIC ESTERS

Catalysts for oxidative esterification can be used, for example, fro converting (meth)acrolein to methyl (meth)acrylate. The catalysts are especially notable for high mechanical and chemical stability even over very long time periods, including activity and/or selectivity relatively in continuous operation in media having even a small water content. 1. A hydrolysis-resistant catalyst , comprising:a) 0.01 to 10 mol % of gold,b) 40 to 94 mol % of silicon,c) 3 to 40 mol % of aluminium, andd) 2 to 40 mol % of at least one element selected from the group consisting of alkali metals, alkaline earth metals, lanthanoids having atomic numbers 57 to 71, Y, Sc, Ti, Zr, Cu, Mn, Pb and Bi,wherein components b) to d) are present as oxides and the stated amounts of components a) to d) relate to 100 mol % of the composition of the catalyst without oxygen,wherein the catalyst is in the form of particles and is suitable for the oxidative esterification of aldehydes to carboxylic esters,wherein the catalyst has a shell structure comprising a core and at least one shell, where at least 80% of the total amount of component a) is part of a shell, andwherein the catalyst has a PZC value between 7 and 11.2. The catalyst according to claim 1 , which claim 1 , except for the oxygen claim 1 , consists of components a) to d).3. The catalyst according to claim 1 , wherein the catalyst comprises between 0.05 and 2 mol % of component a).4. The catalyst according to claim 1 , wherein component a) is in the form of particles having a mean diameter between 2 and 10 nm.5. The catalyst according to claim 1 , wherein the catalyst particles have an average diameter between 10 and 200 μm and a spherical shape.6. The catalyst according to claim 1 , wherein the catalyst comprises between 2 and 30 mol % of Mg claim 1 , Ce claim 1 , La claim 1 , Y claim 1 , Zr claim 1 , Mn claim 1 , Pb and/or Bi as component d).7. The catalyst according to claim 1 , wherein the catalyst has a core and two shells claim 1 , ...

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

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

Process for Converting Butanol into Propylene

Process for selective the conversion of primary C4 alcohol into propylene comprising: contacting a stream () containing essentially a primary C4 alcohol with at least one catalyst at a temperature ranging from 150° C. to 500° C. and at pressure ranging from 0.01 MPa to 10 MPa conditions effective to transform said primary C4 alcohol into an effluent stream () containing essentially propylene, carbon monoxide and di-hydrogen, said transformation of primary C4 alcohol comprising at least a reaction of decarbonylation and optionally a decarboxylation reaction, said at least one catalyst comprising a support being a non-acidic i.e. having a TPD NH3 of less than 50 preferably less than 40 μmol/g and optionally a non-basic catalyst i.e. having a TPD CO2 of less than 100 preferably less than 50 μmol/g. 115.-. (canceled)16. A process for the conversion of primary C4 alcohol into propylene comprising:{'b': 1', '2', '5, 'contacting a stream () containing a primary C4 alcohol with at least one catalyst at a temperature ranging from 150° C. to 500° C. and at pressure ranging from 0.01 MPa to 10 MPa to transform the primary C4 alcohol into an effluent stream (, ) containing propylene, carbon monoxide and di-hydrogen, the transformation of primary C4 alcohol comprising at least a reaction of decarbonylation and optionally a decarboxylation reaction, the at least one catalyst comprising support which is non-acidic, having a TPD NH3 of less than 50 μmol/g and which is also a non-basic, having a TPD CO2 of less than 100 μmol/g.'}17125. The process according to wherein stream () is contacted with the at least one catalyst to produce an effluent stream ( claim 16 , ) wherein at least 1 wt % of primary C4 alcohol is converted into propylene claim 16 , carbon monoxide and di-hydrogen.181121. The process according to claim 16 , wherein the step of contacting the primary C4 alcohol stream () with the at least one catalyst is performed in a single reaction zone (A) and the at least one ...

METHOD FOR PRODUCING UNSATURATED HYDROCARBON

A method for producing an unsaturated hydrocarbon, comprising: a step of contacting a raw material gas containing an alkane with a dehydrogenation catalyst to obtain a product gas containing at least one unsaturated hydrocarbon selected from a group consisting of olefins and conjugated dienes, wherein the dehydrogenation catalyst contains at least one additive element selected from the group consisting of Na, K, and Ca, Al, Mg, a group 14 metal element, and Pt, and a content of the additive element is 0.05% by mass or more and 0.70% by mass or less based on a total mass of the dehydrogenation catalyst. 1. A method for producing an unsaturated hydrocarbon , comprising:a step of contacting a raw material gas containing an alkane with a dehydrogenation catalyst to obtain a product gas containing at least one unsaturated hydrocarbon selected from a group consisting of olefins and conjugated dienes, whereinthe dehydrogenation catalyst contains at least one additive element selected from a group consisting of Na, K, and Ca, Al, Mg, a group 14 metal element, and Pt, anda content of the additive element is 0.05% by mass or more and 0.70% by mass or less based on a total mass of the dehydrogenation catalyst.2. The method according to claim 1 , wherein the content of the additive element is 0.08% by mass or more and 0.35% by mass or less claim 1 , based on the total mass of the dehydrogenation catalyst.3. The method according to claim 1 , wherein a molar ratio of the Mg to the Al is 0.30 or more and 0.60 or less.4. The method according to claim 1 , wherein a molar ratio of the group 14 metal element to the Pt is 10 or less.5. The method according to claim 1 , wherein the group 14 metal element includes Sn.6. The method according to claim 1 , wherein the alkane is an alkane having 4 to 10 carbon atoms.7. The method according to claim 1 , wherein the alkane is butane claim 1 , the olefin is butene claim 1 , and the conjugated diene is butadiene. The present invention relates to ...

A CATALYST COMPOSITION AND ITS APPLICATIONS THEREOF

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

Carbon supported catalyst comprising a modifier and process for preparing the carbon supported catalyst

The invention is related to a carbon supported catalyst comprising a carbon-comprising support with a BET surface area in a range from 400 m 2 /g to 2000 m 2 /g, a modifier comprising at least one mixed metal oxide, comprising niobium and titanium, and/or a mixture, comprising niobium oxide and titanium oxide, a catalytically active metal compound, wherein the catalytically active metal compound is platinum or an alloy comprising platinum and a second metal or an intermetallic compound comprising platinum and a second metal, the second metal being selected from the group consisting of cobalt, nickel, chromium, copper, palladium, gold, ruthenium, scandium, yttrium, lanthanum, niobium, iron, vanadium and titanium. The invention is further related to a process for preparing the carbon supported catalyst.

METHOD OF PRODUCING AN AROMATIZATION CATALYST

According to the subject matter of the present disclosure, a method of producing an aromatization catalyst may comprise producing a plurality of uncalcined ZSM-5 nanoparticles via a dry-gel method, directly mixing the plurality of uncalcined ZSM-5 nanoparticles with large pore alumina and a binder to form a ZSM-5/alumina mixture, and calcining the ZSM-5/alumina mixture to form the aromatization catalyst. The plurality of uncalcined ZSM-5 nanoparticles may have an average diameter of less than 80 nm. 1. A method of producing an aromatization catalyst , the method comprising:producing a plurality of uncalcined ZSM-5 nanoparticles via a dry-gel method,wherein the plurality of ZSM-5 nanoparticles has an average diameter of less than 80 nm;directly mixing the plurality of uncalcined ZSM-5 nanoparticles with large pore alumina and a binder to form a ZSM-5/alumina mixture; andcalcining the ZSM-5/alumina mixture to form the aromatization catalyst; wherein the large pore alumina has a pore size of from 18 nm to 26 nm.2. The method of producing an aromatization catalyst of claim 1 , wherein the plurality of uncalcined ZSM-5 nanoparticles has not been subjected to centrifugation above 3 claim 1 ,000 rpm claim 1 , before being mixed with the large pore alumina and binder.3. The method of producing an aromatization catalyst of claim 1 , wherein the plurality of uncalcined ZSM-5 nanoparticles has not been subjected to calcination above 200° C. for more than 30 minutes claim 1 , before being mixed with the large pore alumina and binder.4. The method of producing an aromatization catalyst of claim 1 , wherein the ZSM-5/alumina mixture is calcined at a temperature of from 400° C. to 700° C. for from 1 hour to 10 hours.5. The method of producing an aromatization catalyst of claim 1 , wherein the aromatization catalyst is impregnated with gallium atoms to form a Ga-ZSM-5 catalyst.6. The method of producing an aromatization catalyst of claim 5 , wherein the Ga-ZSM-5 catalyst is ...

Procedimiento de obtencion de una formulacion catalitica para la produccion de diesel de ultrabajo azufre, el producto obtenido y su aplicacion

The present invention relates to a catalytic formulation used in the hydroprocessing of light and middle oil fractions, preferably in hydrodesulfurization and hydrodenitrogenation reactions to obtain diesel with ultra low sulfur content less than or equal to 15 ppm in weight. The catalytic formulation, object of the present invention, consists of at least one metal of Group VI B and at least one metal of Group VIII B and one element of Group V A of the periodic table deposited on a support based on surface modified alumina with an inorganic oxide of a metal of Group II A, IV A and/or IV B. And containing an impregnated organic compound containing at least one hydroxyl group and at least one carboxyl group and that can contain or not at least one sulfide group in its structure. The catalytic formulation, object of the present invention, allows processing of the oil fractions with initial and final boiling temperatures between 150 and 450° C., with initial nitrogen and sulfur content between 1 and 3% by weight and 200 to 600 ppm, respectively, reducing sulfur content to concentrations lower or equal to 15 ppm and nitrogen concentrations to lower than 1 ppm.

Photocatalytic element for purification and disinfection of air and water and method for the production thereof

The invention relates to the purification and disinfection of air and water. A photocatalytic element consists of sintered glass beads with a pore volume fraction from 20% to 40% and a pore size from 0.1 to 0.5 mm, the surface of which is coated with a titanium dioxide powder, having a specific surface area of 150-400 m 2 /g, at the rate of 0.5-2% relative to the total mass of the photocatalytic element. The surface of the glass beads has a relief shape with a relief depression of 0.5-10 pm. The method for producing the photocatalytic element comprises sintering the glass beads at a temperature that is 5-20° C. higher than the glass softening temperature, modifying the bead surface with chemical etching agents, and coating the bead surface with the titanium dioxide powder from a water suspension at a pH of 2.9±0.1.

SELECTIVE CATALYTIC REDUCTION CATALYST COMPOSITION

A SCR catalyst composition comprises a SCR catalyst; and a binder comprising a porous inorganic material, wherein the porous inorganic material comprises a disordered arrangement of delaminated layers, has a disordered porous structure, and has a multimodal pore size distribution comprising at least a first modal maximum having a macroporous or mesoporous pore size and a second modal maximum having a microporous pore size. The SCR catalyst composition can be manufactured using the method comprising the steps of: (i) providing an inorganic material having a layered structure; (ii) contacting the material with a cationic surfactant to form a swollen material; (iii) agitating the swollen material to form an agitated material; and (iv) calcining the agitated material to recover a delaminated inorganic material, wherein an SCR catalyst is mixed with the inorganic material prior to step (iv). 1. A selective catalytic reduction (SCR) catalyst composition comprising:a SCR catalyst; anda binder comprising a porous inorganic material,wherein the porous inorganic material comprises a disordered arrangement of delaminated layers, has a disordered porous structure, and has a multimodal pore size distribution comprising at least a first modal maximum having a macroporous or mesoporous pore size and a second modal maximum having a microporous pore size.2. The SCR catalyst composition of claim 1 , wherein the multimodal pore size distribution is bimodal.3. The SCR catalyst composition of claim 1 , wherein a powder X-ray diffraction pattern of the porous inorganic material obtained using Cu Kα radiation is devoid of peaks at 2θ values of 10° or less.4. The SCR catalyst composition of claim 1 , wherein the first modal maximum has a mesoporous and/or macroporous pore size.5. The SCR catalyst of claim 1 , wherein the delaminated layers are delaminated silicate layers.6. The SCR catalyst composition of claim 1 , wherein the porous inorganic material comprises one or more of: a clay ...

MATERIALS AND METHODS FOR OXIDATIVE DEHYDROGENATION OF ALKYL AROMATIC COMPOUNDS INVOLVING LATTICE OXYGEN OF TRANSITION METAL OXIDES

In one aspect, the disclosure relates to a process for dehydrogenating a first dehydrogenation reactant into its unsaturated counterparts. The disclosed process comprises introducing a dehydrogenation reactant to a metal oxide catalyst having dehydrogenation activity, and dehydrogenating the dehydrogenation reactant to provide its unsaturated counterpart and hydrogen; selectively combusting the hydrogen released during dehydrogenation using a lattice oxygen from the metal oxide catalyst, resulting in a reduced metal oxide catalyst and steam; re-oxidizing the reduced metal oxide catalyst by introducing a gaseous oxidant to the reduced metal oxide catalyst; and optionally re-using the re-oxidized metal oxide catalyst for catalytic conversion and combustion. This abstract is intended as a scanning tool for purposes of searching in the particular art and is not intended to be limiting of the present disclosure. 1. A process for oxidative dehydrogenation , comprising:a. introducing one or more dehydrogenation reactants to a metal oxide catalyst having dehydrogenation activity, and dehydrogenating the one or more dehydrogenation reactants to provide a dehydrogenated reaction product and hydrogen;b. selectively combusting the hydrogen released during dehydrogenation using a lattice oxygen from the metal oxide catalyst, resulting in a reduced metal oxide catalyst and steam;c. re-oxidizing the reduced metal oxide catalyst by introducing a gaseous oxidant to the reduced metal oxide catalyst; and optionallyd. re-using the re-oxidized metal oxide catalyst for a subsequent dehydrogenation and/or selective combustion.2. The process of claim 1 , wherein the dehydrogenation reactants comprise an alkyl aromatic hydrocarbon or a substituted alkyl aromatic hydrocarbon and the dehydrogenated reaction product comprises an alkene aromatic hydrocarbon or substituted alkene aromatic hydrocarbon claim 1 , respectively.3. The process of claim 1 , wherein the dehydrogenation reactants ...

CONTROLLED HEIGHT CARBON NANOTUBE ARRAYS

Controlled height carbon nanotube arrays including catalysts and synthesis methods relating thereto are disclosed. Such nanotube arrays can be prepared from catalyst particles having an Fe:Co:Ni molar ratio impregnated in an exfoliated layered mineral to grow carbon nanotube arrays where the Fe:Co:Ni molar ratio of the catalyst is used to control the height of the array. 1. A method for growing a carbon nanotube array , the method comprising:soaking an exfoliated layered mineral in a metal ion aqueous solution comprising an iron salt, a cobalt salt, and a nickel salt to produce an impregnated layered mineral;calcining the impregnated layered mineral to produce a supported catalyst; andgrowing a carbon nanotube array on the supported catalyst.2. The method of claim 1 , wherein a molar ratio of iron to cobalt in the metal ion aqueous solution is about 200:1 to about 1:5 claim 1 , a molar ratio of iron to nickel in the metal ion aqueous solution is about 200:1 to about 1:5 claim 1 , and a molar ratio of cobalt to nickel in the metal ion aqueous solution is about 10:1 to about 1:10.3. The method of claim 1 , wherein the metal ion aqueous solution further comprises salts of one or more of Mo claim 1 , W claim 1 , Al claim 1 , Mg and combinations thereof.4. The method of claim 1 , wherein the metal ion aqueous solution further comprises: (i) a salt of Mo or W or a combination thereof and (ii) a salt of Al or Mg or a combination thereof.5. The method of claim 1 , wherein the iron salt comprises at least one selected from the group consisting of: iron (II) nitrate claim 1 , iron (III) nitrate claim 1 , iron (II) chloride claim 1 , iron (III) chloride claim 1 , iron (II) bromide claim 1 , iron (III) bromide claim 1 , iron (II) fluoride claim 1 , iron (III) fluoride claim 1 , iron (II) sulfate claim 1 , iron (III) sulfate claim 1 , and any combination thereof.6. The method of claim 1 , wherein the cobalt salt comprises at least one selected from the group consisting of: ...

Catalyst for dehydration reaction of primary alcohols, method for preparing the same and method for preparing alpha-olefins using the same

Provided are a catalyst for dehydration reaction of a primary alcohol, a method for preparing the same, and a method for preparing alpha-olefins using the same. According to the present invention, there is provided a catalyst for dehydration reaction of primary alcohols capable of adjusting the strength and distribution of Lewis acid sites (LASs) on a surface of an alumina catalyst to realize high selectivity to alpha-olefins as well as a high conversion rate in the dehydration reaction of primary alcohols. Therefore, high-purity alpha-olefins having a low isomeric yield fraction as well as a high conversion rate can be produced from the primary alcohols.

CATALYTIC BODY COATED WITH METAL OXIDE, METHOD OF MANUFACTURING THE SAME, AND METHOD OF PREPARING 1,3-BUTADIENE USING THE SAME

According to an embodiment of the present invention, there are provided a catalytic body, a method of manufacturing the same, and a method of preparing 1,3-butadiene using the same. The catalytic body includes an inactive support; an intermediate layer disposed on a surface of the inactive support; and an active layer disposed on a surface of the intermediate layer, wherein the active layer includes catalyst powder and a binder. 1. A catalytic body comprising:an inactive support;an intermediate layer disposed on a surface of the inactive support; andan active layer disposed on a surface of the intermediate layer,wherein the active layer includes catalyst powder and a binder.2. The catalytic body of claim 1 , wherein the inactive support has a porosity of 70 vol % or less.3. The catalytic body of claim 2 , wherein the inactive support is of one shape selected from the group consisting of a spherical shape claim 2 , a cylindrical shape claim 2 , a ring shape claim 2 , a platy shape claim 2 , and a combination of two or more thereof.4. The catalytic body of claim 3 , wherein the inactive support is one selected from the group consisting of alumina claim 3 , silica claim 3 , zirconia claim 3 , silicon carbide claim 3 , cordierite claim 3 , and a combination of two or more thereof.5. The catalytic body of claim 1 , wherein the intermediate layer may consist of one selected from the group consisting of alumina claim 1 , silica claim 1 , kaolin claim 1 , TiO claim 1 , ZnO claim 1 , bentonite claim 1 , and a combination of two or more thereof.6. The catalytic body of claim 1 , wherein the intermediate layer has a weight of 3 to 15 g/L with respect to a volume of the inactive support.7. The catalytic body of claim 1 , wherein the catalyst powder is an oxide derived from one selected from the group consisting of iron claim 1 , magnesium claim 1 , manganese claim 1 , zinc claim 1 , bismuth claim 1 , molybdenum claim 1 , and a combination of two or more thereof.8. The catalytic ...

MULTIMETALLIC CATALYSTS FOR METHANATION OF CARBON DIOXIDE AND DRY REFORMING OF METHANE

Processes for forming multimetallic catalysts by grafting nickel precusors to metal oxide supports. Dry reforming reaction catalysts having nickel and promotors grafted to metal oxides supports. Methanation reaction catalysts having nickel and promotors grafted to metal oxides supports. 1. A method of forming a multimetallic catalyst comprising:{'sub': 2', '3', '2', '2', '2, 'grafting an organometallic promotor comprising a metal selected from the group consisting of B, Cu, Co, Fe, Mn, Sn, Mg, V, and Zn and an organic ligand, onto a metal oxide support selected from the group consisting of AlO, CeO, MgO, SiO, and TiO, forming a promotor-support material;'}calcine the organometallic promotor in air to form a calcined promotor-support material;grafting an organonickel precursor grafted onto the calcined promotor-support material; andreducing the organonickel grafted promotor-support material to form an active multimetallic catalyst.2. The method of claim 1 , wherein reducing comprises reduction with 5-20% hydrogen at 200-600° C. for 2 hours and the active multimetallic catalyst is a methanation reaction catalyst.3. The method of claim 2 , wherein reducing comprises reduction with 10% hydrogen at 500° C. for 2 hours.4. The method of claim 2 , wherein the metal oxide support comprises CeO.5. The method of claim 4 , wherein the metal is selected from the group consisting of B claim 4 , Co claim 4 , Mn claim 4 , Sn claim 4 , and V.6. The method of claim 1 , wherein the wherein the oxide support comprises AlO.7. The method of claim 4 , wherein the metal is selected from the group consisting of Mg and V.8. The method of claim 1 , wherein reducing comprises reduction with 5-20% hydrogen at 700-850° C. for 2 hours and the active multimetallic catalyst is a dry reforming reaction catalyst.9. The method of claim 1 , wherein reducing comprises reduction with 10% hydrogen at 800° C. for 2 hrs.10. The method of claim 8 , wherein the wherein oxide support is selected from the group ...

SINGLE STEP PROCESS FOR THE SIMULTANEOUS PRODUCTION OF AROMATICS, NAPHTHENICS AND ISOPARAFFINS USING TRANSITION METAL FUNCTIONALIZED ZEOLITE BASED CATALYST

Hydrocarbon composition plays vital role in fuel quality. For gasoline/motor spirit applications the hydrocarbon should have more octane-possessing molecules from the groups of aromatics, naphthenics and isoparaffins, while n-paraffins are not preferred due to their poor octane. Among the high-octane groups, again aromatics occupy the top but not more than 35 vol % aromatics can be mixed in gasoline for engine applications to avoid harmful emission, But there is no single process that addresses so far the issue of co-producing all the desired hydrocarbon components in a single process. Thus, it is interesting to have a single once-through process working on single catalyst system to produce mixture of all three high-octane molecules namely, aromatics, naphthenics and isoparaffins directly from low-value, low-octane n-paraffin feed. Herein, we report a novel single-step catalytic process for the simultaneous production of aromatics, naphthenics and isoparaffins for gasoline and petrochemical applications. 1. A transition metal functionalized zeolite based catalyst comprising: a binder and a HZSM-5 zeolite in a weight ratio of zeolite:binder as 3:2;wherein the HZ SM-5 zeolite has a framework of silicon and aluminium in a ratio of 100-300; andwherein the catalyst possesses both acidity and dehydrogenation functionalities for simultaneous production of aromatics and isoparaffins.2. The catalyst as claimed in claim 1 , wherein the binder is an inert alumina binder claim 1 , preferably pseudo boehmite.3. The catalyst as claimed in claim 1 , wherein the transition metal is selected from platinum cobalt claim 1 , or a combination thereof.4. The catalyst as claimed in claim 1 , wherein surface area of the catalyst is in the range of 350-430 m/g claim 1 , total pore volume is in the range of 0.32-0.37 cm/g claim 1 , and average particle size is in the range of 139-170 Å.5. A process for preparation of a transition metal functionalized zeolite based catalyst possessing both ...

USE OF A BIFUNCTIONAL CATALYST BASED ON ZEOLITE IZM-2 FOR THE HYDROISOMERIZATION OF LIGHT PARAFFINIC FEEDSTOCKS RESULTING FROM FISCHER-TROPSCH SYNTHESIS

A process is described for producing middle distillates from a paraffinic feedstock produced by Fischer-Tropsch synthesis and divided into a light fraction (cold condensate) and a heavy fraction (waxes). The process involves fractionation of the waxes to obtain a light fraction, the final boiling point of which is between 350° C. and 400° C., and a heavy fraction which boils above the light fraction. The light fraction is mixed with at least one portion of the cold condensate. The resultant mixture is hydrotreated in the presence of a hydrotreatment catalyst of at least one portion of the resultant effluent is hydroisomerized in the presence of a catalyst comprising at least one noble metal from Group VIII and at least one zeolite IZM-2. At least one portion of the heavy fraction is subjected to hydrocracking and hydroisomerization in the presence of a hydrocracking catalyst. The resultant effluents are fractionated to obtain at least one middle distillates fraction. 1. Process for producing middle distillates from a paraffinic feedstock produced by Fischer-Tropsch synthesis and divided into two fractions , a light fraction , known as cold condensate , and a heavy fraction , known as waxes , comprising at least the following steps:a) fractionation of said heavy fraction, known as waxes, so as to obtain a light fraction of the waxes, the final boiling point of which is between 350° C. and 400° C., and a heavy fraction which boils above said light fraction,b) mixing of said light fraction, the final boiling point of which is between 350° C. and 400° C. and preferably between 360° C. and 380° C., and preferably less than 370° C., derived from step a) with at least one portion of said cold condensate fraction,{'sup': '−1', 'c) hydrotreatment of the mixture derived from step b) in the presence of a hydrotreatment catalyst and which operates at a temperature of between 250 and 450° C., at a pressure of between 0.5 and 15 MPa, at a hydrogen flow rate adjusted in order to ...

Catalyst Supports and Catalyst Systems and Methods

Provided herein are catalyst supports, catalyst systems, and methods for making catalyst supports, catalyst systems, and performing chemical reactions with the catalyst systems. The catalyst supports include a zeolite and a binder including non-sodium counterions, such as ammonium counterions and/or potassium counterions. The catalyst systems include the catalyst supports and a catalytic material. The catalyst systems may be used to perform chemical reactions, including reactions of one or more hydrocarbons. 1. A process for making a catalyst support , the process consisting essentially of:contacting a zeolite and a binder to form a mixture, wherein the binder comprises a colloidal silica including potassium counterions, ammonium counterions, or a combination thereof, and substantially no sodium counterions;extruding and/or shaping the mixture to form a dimensioned mixture;drying the dimensioned mixture to form a substantially dried dimensioned mixture; andcalcining the substantially dried dimensioned mixture to produce the catalyst support.2. The process of claim 1 , wherein the mixture further comprises an extrusion aid.3. The process of claim 2 , wherein the extrusion aid comprises a cellulose ether.4. The process of claim 3 , wherein the cellulose ether comprises ethylcellulose claim 3 , carboxymethylcellulose claim 3 , ethylhydroxyethylcellulose claim 3 , hydroxyethylcellulose claim 3 , hydroxypropylcellulose claim 3 , methylhydroxyethylcellulose claim 3 , methylhydroxypropylcellulose claim 3 , or a combination thereof.5. The process of claim 1 , wherein the mixture further comprises water in an amount sufficient to permit the mixture to form the dimensioned mixture upon the extruding and/or shaping.6. The process of claim 1 , wherein the zeolite comprises a large pore zeolite.7. The process of claim 6 , wherein the large pore zeolite has an effective pore diameter of from about 6 Angstroms (Å) to about 15 Å.8. The process of claim 1 , wherein the zeolite is ...

Carrier for synthesis gas production catalyst, method of manufacturing the same, synthesis gas production catalyst, method of manufacturing the same and method of producing synthesis gas

This invention provides a carrier for a synthesis gas production catalyst that can suppress carbon depositions and allows to efficiently produce synthesis gas on a stable basis for a long duration of time when producing synthesis gas by carbon dioxide reforming. It is a carrier to be used for producing synthesis gas containing carbon monoxide and hydrogen from source gas containing methane-containing light hydrocarbons and carbon dioxide. The carrier contains magnesium oxide grains and calcium oxide existing on the surfaces of magnesium oxide grains. The calcium oxide content thereof is between 0.005 mass % and 1.5 mass % in terms of Ca.

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

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

PREPARATION METHOD OF PLATINUM/TIN/METAL/ALUMINA CATALYST FOR DIRECT DEHYDROGENATION OF n-BUTANE AND METHOD FOR PRODUCING C4 OLEFINS USING SAID CATALYST

The provided is a method for preparing a platinum-tin-metal-alumina catalyst by comprising: as an active ingredient, platinum which has a high activity in a direct dehydrogenation reaction of n-butane, tin which can increase the catalyst stability by preventing carbon deposition; additionally metal for reducing the level of catalyst inactivation over the reaction time; and an alumina carrier for supporting said components. Further, provided is a method for producing a high value product, C4 olefins from low cost n-butane by using the catalyst prepared by the method according to the present invention in a direct dehydrogenation reaction.

METHOD FOR PRODUCING COMPOSITE OXIDE AND COMPOSITE OXIDE CATALYST

Provided are a method for producing a composite oxide and the composite oxide. The method includes steps of: (a) preparing a Ce aqueous solution not less than 80 mol % of which Ce ions are tetravalent, and a Zr aqueous solution; (b1) mixing the Zr aqueous solution and a portion of the Ce aqueous solution to prepare a mixed aqueous solution (X1); (c1) hydrothermally processing the solution (X1); (b2) adding the remainder of the Ce aqueous solution of step (a) to a colloidal solution (Y1) of a composite salt obtained from step (c1) to prepare a colloidal solution (Y2) of a composite salt; (c2) hydrothermally processing the solution (Y2); (d) mixing a colloidal solution (Y3) of a composite salt obtained from step (c2) with an alkaline solution and a surfactant to prepare a precipitate; and (e) calcining the precipitate. 1. A composite oxide obtained by a method comprising the steps of:(a) preparing at least a cerium aqueous solution 80 to 100 mol % of which cerium ions are tetravalent, and a zirconium aqueous solution containing zirconium ions;(b1) mixing said zirconium aqueous solution and a portion of said cerium aqueous solution prepared in step (a) to prepare a mixed aqueous solution (X1);(c1) hydrothermally processing said mixed aqueous solution (X1);(b2) adding a remainder of said cerium aqueous solution prepared in step (a) to a colloidal solution (Y1) of a composite salt obtained by said hydrothermal processing in step (c1) to prepare a colloidal solution (Y2) of a composite salt;(c2) hydrothermally processing said colloidal solution (Y2) of a composite salt obtained from step (b2) ;(d) mixing a colloidal solution (Y3) of a composite salt obtained by said hydrothermal processing in step (c2) with an alkaline solution and a surfactant to prepare a precipitate; and(e) calcining said precipitate,wherein the composite oxide comprises Ce, Zr, Pr, and oxygen, andwherein the content of Zr is not less than 20 mol% and not more than 50 mol %, and the content of Pr is ...

METHOD FOR CATALYTIC AMMONIA SYNTHESIS UNDER CONCENTRATED SOLAR ENERGY AND CATALYSTS

A method for catalytic ammonia synthesis under concentrated solar energy and related catalysts. The method includes placing a catalyst in a reaction apparatus, feeding nitrogen and hydrogen into the reaction apparatus, and controlling a surface temperature of the catalyst to reach about 300° C. to 550° C. under irradiation of concentrated sunshine, to synthesize ammonia. The catalyst includes an amorphous and electron-rich black nano TiO(0 Подробнее

Supported Hydrotreating Catalysts Having Enhanced Activity

This invention provides supported catalysts comprising a carrier, phosphorus, at least one Group VI metal, at least one Group VIII metal, and a polymer. In the supported catalyst, the molar ratio of phosphorus to Group VI metal is about 1:1.5 to less than about 1:12, the molar ratio of the Group VI metal to the Group VIII metal is about 1:1 to about 5:1, and the polymer has a carbon backbone and comprises an amido group. Also provided are a process for preparing such supported catalysts, as well as methods for hydrotreating, hydrodenitrogenation, and/or hydrodesulfurization, using supported catalysts. 1. A supported catalyst comprising a carrier , phosphorus , at least one Group VI metal , at least one Group VIII metal , and a polymer , wherethe molar ratio of phosphorus to Group VI metal is about 1:1.5 to less than about 1:12,the molar ratio of the Group VI metal to the Group VIII metal is about 1:1 to about 5:1, andthe polymer has a carbon backbone and comprises an amido group.2. A supported catalyst as in wherein:said carrier is carbon, carbon in combination with one or more inorganic oxides, boria, titania, silica, alumina, silica-alumina, alumina with silica-alumina dispersed therein, alumina-coated silica, silica-coated alumina, alumina containing boron, alumina containing silicon, alumina containing titanium, or a combination of any two or more of these;the polymer is polyacrylamide, polymethacrylamide, poly(N-isopropyl)acrylamide, poly(N-hydroxymethyl)acrylamide, poly(N-hydroxyethyl)acrylamide, poly(N-methoxymethyl)acrylamide, poly(N-ethoxymethyl)acrylamide, or a co-polymer of any two or more of the foregoing; and/orsaid Group VI metal is molybdenum and/or tungsten, and/or wherein said Group VIII metal is nickel and/or cobalt.3. A supported catalyst as in wherein the polymer is polyacrylamide.4. A supported catalyst as in wherein the molar ratio of phosphorus to Group VI metal is about 1:2.5 to less than about 1:12 claim 1 , and/or wherein the catalyst has a ...

METHODS FOR PREPARATION AND USE OF LIQUID SYNTHESIS CATALYSTS

Described herein are catalysts relating to liquid synthesis, methods of their preparation, and methods of their use. In an embodiment according to the present disclosure, a method of producing a catalyst for liquid synthesis comprises: providing a silica oxide support; pretreating the silica oxide support to remove air and moisture; impregnating the pretreated silica oxide support with cobalt from a cobalt source using a cobalt impregnation method; and calcinating the impregnated silica oxide support in an oven with a temperature ramping profile, wherein the calcinating comprises feeding air into the oven. 1) A method of producing a catalyst for liquid synthesis , comprising:providing a silica oxide support;pretreating the silica oxide support to remove air and moisture;impregnating the pretreated silica oxide support with cobalt from a cobalt source using a cobalt impregnation method; andcalcinating the impregnated silica oxide support in an oven with a temperature ramping profile, wherein the calcinating comprises feeding air into the oven.2) The method of any claim 1 , wherein the silica oxide support comprises silica oxide pellets.3) The method of claim 2 , wherein the silica oxide pellets are cylindrical and have a dimension of about 2 mm to about 4 mm.4) The method of claim 2 , wherein the silica oxide pellets have a packing density of about 20 lbs/ftto about 40 lbs/ft.5) The method of claim 1 , wherein the cobalt source is cobalt nitrate or cobalt chloride.6) The method of claim 1 , wherein the cobalt impregnation method is incipient wet impregnation (IWI).7) The method of claim 1 , further comprising impregnating the cobalt impregnanted support with ruthenium (Ru) from a Ru source with an Ru impregnation method before calcinating.8) The method of claim 7 , wherein the ruthenium impregnation method is incipient wet impregnation (IWI).9) The method of claim 7 , wherein the Ru source is ruthenium chloride or ruthenium nitrate.10) The method of claim 1 , further ...

METHOD FOR SYNTHESIZING N,N'-BIS(2,2,6,6-TETRAMETHYL-4-PIPERIDYL)-1,3-BENZENEDICARBOXAMIDE

The present invention relates to a method for synthesizing N,N′-bis(2,2,6,6-tetramethyl-4-piperidyl)-1,3-benzenedicarboxamide as shown in the following formula (III), 2. The synthetic method according to claim 1 , characterized in that the solid supported catalyst is prepared by a method comprising the following steps:S1: treating a KIT-1 molecular sieve with 120° C. to 130° C. water vapor for 20 to 30 minutes, then naturally cooling to room temperature and thoroughly drying in vacuum to obtain a heat-treated molecular sieve;S2: immersing the heat-treated molecular sieve in a nitric acid aqueous solution with a molar concentration of 0.5 to 0.7 mol/L for 2 to 3 hours and then thoroughly washing with deionized water and completely drying to obtain an acid-treated molecular sieve;S3: preparing a nickel chloride aqueous solution with a molar concentration of 1.0 mol/L and a lanthanum trifluoromethanesulfonate aqueous solution with a molar concentration of 0.4 mol/L respectively;S4: impregnating the acid-treated molecular sieve with the nickel chloride aqueous solution, enabling the mass ratio of adsorbed nickel ions to the heat-treated molecular sieve of Step 1 to be (0.05 to 0.08) to 1, and then completely drying to obtain a nickel ion supported molecular sieve; andS5: impregnating the nickel ion supported molecular sieve with the lanthanum trifluoromethanesulfonate aqueous solution until the molar ratio of the adsorbed lanthanum ions to the adsorbed nickel ions in step S4 is (1.5 to 2.5) to 1, and then completely drying again to obtain the solid supported catalyst.3. The synthetic method according to claim 2 , characterized in that the mass ratio of the adsorbed nickel ions to the heat-treated molecular sieve obtained in step S1 is (0.05 to 0.08) to 1 in step S4.4. The synthetic method according to claim 2 , characterized in that the molar ratio of the adsorbed lanthanum ions to the adsorbed nickel ions in step S4 is (1.5 to 2.5) to 1 claim 2 , most preferably 2 to 1 ...

METHODS OF PREPARING A CATALYST UTILIZING HYDRATED REAGENTS

A method of preparing a catalyst comprising a) contacting a titanium-containing compound, a solvating agent, and a solvent to form a solution; b) contacting the solution with a chrominated silica-support to form a pre-catalyst; and c) thermally treating the pre-catalyst by heating to a temperature of from about 400° C. to about 1000° C. for a time period of from about 1 minute to about 24 hours to form the catalyst. 1. A method of preparing a pre-catalyst comprising:a) contacting (i) a titanium-containing compound, (ii) ascorbic acid or a derivative thereof and (iii) a solvent to form a solution;b) contacting the solution with a chromium-containing compound to form a mixture; andc) spray-drying a silica support with the mixture to form the pre-catalyst.2. The method of wherein the ascorbic acid comprises L-ascorbic acid claim 1 , D-ascorbic acid claim 1 , L-isoascorbic acid claim 1 , D-isoascorbic acid claim 1 , D-erythorbic acid or a combination thereof.3. The method of wherein a weight ratio of ascorbic acid or a derivative thereof to silica of the silica support is from about 0.5:1 to about 10:1.4. The method of wherein the titanium-containing compound provides an amount of titanium in the pre-catalyst of from about 0.01 wt. % to about 10 wt. % based on the weight of the pre-catalyst.5. The method of wherein the titanium-containing compound is characterized by a general formula Ti(OR)(acac)wherein ORis ethoxide claim 1 , isopropoxide claim 1 , n-propoxide claim 1 , butoxide claim 1 , or a combination thereof and “acac” is acetylacetonate.6. The method of wherein the titanium-containing compound is characterized by a general formula Ti(OR)(oxal) wherein ORis ethoxide claim 1 , isopropoxide claim 1 , n-propoxide claim 1 , butoxide claim 1 , or a combination thereof and “oxal” is oxalate.7. The method of wherein the solvent is an aqueous solvent claim 1 , a nonaqueous solvent claim 1 , an alcohol or a combination thereof.8. The method of wherein the solvent is water ...

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

A hydrocracking catalyst is provided comprising: 1. A hydrocracking catalyst comprising:{'sup': '2', 'a. from 0.5 to 10 wt % zeolite beta having an OD acidity of 20 to 400 μmol/g and an average domain size from 800 to 1500 nm;'}b. from 0 to 5 wt % zeolite USY having an ASDI between 0.05 and 0.12; wherein a wt % of the zeolite beta is greater than the wt % of the zeolite USY;c. a catalyst support; andd. 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 hydrocracking catalyst of claim 1 , wherein the zeolite beta has a SiO/AlOmole ratio (SAR) from 50 to 200.3. The hydrocracking catalyst of claim 1 , wherein the OD acidity is from 30 to 100 μmol/g.4. The hydrocracking catalyst of claim 1 , wherein the average domain size is from 900 to 1250 nm.5. The hydrocracking catalyst of claim 1 , wherein the zeolite beta has more large domains that have a domain size from 1200 to 2000 nmthan small domains that have the domain size from 200 to 600 nm.6. The hydrocracking catalyst of claim 1 , wherein the zeolite beta has a standard deviation for domain sizes greater than 700 nm.7. The hydrocracking catalyst of claim 1 , wherein the wt % of the zeolite beta is from 1 to 5 wt % higher than the wt % of the zeolite USY.8. The hydrocracking catalyst of claim 1 , wherein a weight ratio of the zeolite USY to the zeolite beta is 0 to 0.48.9. The hydrocracking catalyst of claim 1 , wherein the zeolite USY has a total Brösted acid sites determined by FTIR after H/D exchange of 0.080 to 0.200 mmol/g.10. The hydrocracking catalyst of claim 1 , comprising at least one Group 6 metal and at least one metal selected from Groups 8 through 10 of the Periodic Table.11. A process for hydrocracking a hydrocarbonaceous feedstock claim 1 , comprising contacting the hydrocarbonaceous feedstock with a hydrocracking catalyst under hydrocracking conditions to produce a hydrocracked effluent that comprises middle distillates; ...

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

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

NOBLE METAL ZEOLITE CATALYST FOR SECOND-STAGE HYDROCRACKING TO MAKE MIDDLE DISTILLATE

A second-stage hydrocracking catalyst is provided, comprising: a) a zeolite beta having an OD acidity of 20 to 400 nmol/g and an average domain size from 800 to 1500 nm2; b) a zeolite USY having an ASDI between 0.05 and 0.12; c) a catalyst support; and d) 0.1 to 10 wt % noble metal; wherein the second-stage hydrocracking catalyst provides a hydrogen consumption less than 350 SCFB across a range of synthetic conversions up to 37 wt % when used to hydrocrack hydrocarbonaceous feeds having an initial boiling point greater than 380° F. (193° C.). A second-stage hydrocracking process using the second-stage hydrocracking process is provided. A method to make the second-stage hydrocracking catalyst is also provided. 1. A second-stage hydrocracking catalyst , comprising:{'sup': '2', 'a. a zeolite beta having an OD acidity of 20 to 400 μmol/g and an average domain size from 800 to 1500 nm;'}b. a zeolite USY having an ASDI between 0.05 and 0.12;c. a catalyst support; andd. 0.1 to 10 wt % noble metal; wherein the second-stage hydrocracking catalyst provides a hydrogen consumption less than 350 SCFB across a range of synthetic conversions up to 37 wt % when used to hydrocrack hydrocarbonaceous feeds having an initial boiling point greater than 380° F. (193° C.).2. The second-stage hydrocracking catalyst of claim 1 , wherein a wt % of the zeolite beta is greater than the wt % of the zeolite USY.3. The second-stage hydrocracking catalyst of claim 1 , wherein the OD acidity is from 30 to 100 μmol/g.4. The second-stage hydrocracking catalyst of claim 1 , wherein the average domain size is from 900 to 1250 nm.5. The second-stage hydrocracking catalyst of claim 1 , wherein the zeolite USY has a total Brönsted acid sites determined by FTIR after H/D exchange of 0.080 to 0.200 mmol/g.6. The second-stage hydrocracking catalyst of claim 1 , wherein the second-stage hydrocracking catalyst has the hydrogen consumption between 250 and 350 SCFB over the range of synthetic conversion<625° F. ...

SINGLE ATOM CATALYST AND METHOD OF FORMING THE SAME

A single atom catalyst and a method of forming the same are provided. The single atom catalyst comprises a support comprising a first metal oxide and a second metal atom located in the first metal oxide. The method of forming the single atom catalyst comprises forming a sacrificial nanoparticle, coating the sacrificial nanoparticle with a first metal oxide, adsorbing a second metal atom to the first metal oxide, forming a sacrificial layer on the support, and heating the first metal oxide. 1. A single atom catalyst comprising:a support comprising a first metal oxide; anda second metal atom located in the first metal oxide.2. The single atom catalyst of claim 1 , wherein the second metal atom is located in a first metal vacancy in the first metal oxide.3. The single atom catalyst of claim 1 , wherein the first metal oxide comprises Tice .4. The single atom catalyst of claim 1 , wherein the second metal comprises a transition metal.5. The single atom catalyst of claim 4 , wherein the second. metal comprises at least one of Cu claim 4 , Fe claim 4 , Co claim 4 , Ni claim 4 , and Rh.6. The single atom catalyst of claim 1 , wherein the support has a hollow spherical shape.7. The single atom catalyst of claim 1 , wherein the first metal oxide has crystalline property.81. The single atom catalyst of claim claim 1 , claim 1 , wherein the single atom catalyst is activated by light irradiation and deactivated by exposure to oxygen.9. A method of forming a single atom catalyst comprising:forming a sacrificial nanoparticle;coating the sacrificial nanoparticle with a first metal oxide;adsorbing a second metal atom to the first metal oxide;forming a sacrificial layer on the support; andheating the first metal oxide.10. The method of claim 9 , wherein the sacrificial nanoparticle and the sacrificial layer is formed with SiO.11. The method of claim 9 , wherein the first metal oxide comprises TiO.12. The method of claim 9 , wherein the second metal comprises a transition metal.1312. ...

Metal complex of fluorinated tin oxide and titanium oxide and preparation method thereof

Disclosed is a metal complex including: a tin oxide; titanium oxide nanorods in a rutile phase formed on the tin oxide; and titanium oxide nanoparticles in an anatase phase formed on the titanium oxide nanorods in a rutile phase, and a preparation method thereof, and can be used as a catalyst support in various forms.

Processes for producing beta-lactone and beta-lactone derivatives with heterogenous catalysts

The present invention is directed to processes from producing beta-lactone and beta-lactone derivatives using heterogenous catalysts. In preferred embodiments of the present invention, the processes comprise the steps: passing a feed stream comprising an epoxide reagent and a carbon monoxide reagent to a reaction zone; contacting the epoxide reagent and the carbon monoxide reagent with a heterogenous catalyst to produce a beta-lactone product in the reaction zone; and removing the beta-lactone product from the reaction zone. In preferred embodiments, the heterogenous catalyst comprises a solid support containing a cationic Lewis acid functional group and a metal carbonyl compound comprising at least one of anionic metal carbonyl compound or a neutral metal carbonyl compound. In certain preferred embodiments, the epoxide reagent and carbon monoxide reagent have a biobased content.

PROCESS FOR PREPARING A HYDRO-TREATING CATALYST COMPOSITION FOR PRODUCING ULTRA-LOW SULFUR DIESEL

A process for preparation of catalyst to produce ultra-low sulfur diesel (ULSD) from high refractory sulfur feedstock. The catalyst composition comprises a modified alumina carrier, impregnated by metal of group VIB is in the range of 15-25% and metal of group VIIIB is in the range of 1-5% as oxides. The catalyst prepared in the present invention produces highly dispersed MoS2 active sites on the modified carrier. The catalyst produces ultra low sulfur diesel (ULSD) along with improved cetane, density reduction and endpoint reduction. 2. The process as claimed in claim 1 , wherein alumina powder is selected from the group boehmite alumina claim 1 , pseudo-boehmite alumina claim 1 , gamma alumina claim 1 , alpha alumina claim 1 , and mixtures thereof.3. The process as claimed in claim 1 , wherein extrudates of step b are dried at 100-130° C. for 8-16 hours and calcinated in air at 450-600° C. for 1-5 hrs.4. The process as claimed in claim 1 , wherein the inorganic acid used for peptizing is selected from a group consisting of nitric acid claim 1 , hydrochloric acid claim 1 , formic acid claim 1 , sulfuric acid claim 1 , or a mixture thereof in a concentration range of 0.5-3 wt % of alumina powder.5. The process as claimed in claim 1 , wherein organic additive of step (c) is selected from a group of glycol claim 1 , glycerol claim 1 , and sorbitol claim 1 , in a range of 1 to 20% wt of the total weight of the carrier claim 1 , preferably 5 to 10% wt.6. The process as claimed in claim 1 , wherein metal of group VIB is in the range of 15-25% whereas the metal from group VIIIB is in the range of 1-5% as oxides of the total weight of the catalyst composition.7. The process as claimed in claim 1 , wherein the Group VIIIB metal is selected from Ni or Co and wherein the Group VIB metal is selected from Mo or W.8. The process as claimed in claim 1 , wherein organic additive of step (e) is selected from amine group containing compounds such as ethylamine claim 1 , ethanolamine ...

FILM SYSTEM AND METHOD OF FORMING SAME

A film system includes a substrate and a film disposed on the substrate. The film includes a monolayer formed from a fluorocarbon and a plurality of regions disposed within the monolayer such that each of the plurality of regions abuts and is surrounded by the fluorocarbon. Each of the plurality of regions includes a photocatalytic material. A method of forming a film system includes depositing a monolayer formed from a fluorocarbon onto a substrate. After depositing, the method includes ablating the monolayer to define a plurality of cavities therein, wherein each of the plurality of cavities is spaced apart from an adjacent one of the plurality of cavities along the monolayer. After ablating, the method includes embedding a photocatalytic material into each of the plurality of cavities to form a film on the substrate and thereby form the film system. 1. A film system comprising:a substrate; and a monolayer formed from a fluorocarbon; and', 'a plurality of regions disposed within the monolayer such that each of the plurality of regions abuts and is surrounded by the fluorocarbon, wherein each of the plurality of regions includes a photocatalytic material., 'a film disposed on the substrate and including2. The film system of claim 1 , wherein the film has a first surface and a second surface spaced opposite the first surface and abutting the substrate claim 1 , and further wherein the first surface is substantially free from squalene.3. The film system of claim 2 , wherein the plurality of regions are equally spaced apart from each other along the first surface.4. The film system of claim 2 , wherein the substrate has:a proximal surface abutting the second surface;a distal surface spaced opposite the proximal surface;a first edge connecting the proximal surface and the distal surface; anda second edge spaced opposite the first edge; andfurther including a light source disposed adjacent the first edge and configured for emitting electromagnetic radiation.5. The film ...

Carbon-based noble metal-transition metal catalyst enabling high selective conversion and production method therefor

Provided are a carbon-based noble metal-transition metal composite catalyst enabling high selective conversion of a carboxylic acid functional group into an alcohol functional group by pre-treating a carbon carrier including a predetermined ratio or more of mesopores, and a production method therefor.

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

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

Method for the Fixation of Metals, Transition Metals and their Oxides on Siliceous Materials of Plant Origin and Use of these Modified Siliceous Materials as a Catalyst and a Loading Material for Pigments, Paints, Plastics, Elastomers and Sizing Materials

The invention relates to a method, in which siliceous biomass is modified in the spectrum of the existing non-silicon metals and these non-silicon metals are fixed onto the siliceous skeleton of the plant by burning. The ashes produced can be used as auxiliary agents for heterogeneous catalysis in the chemical industry and as loading materials for plastics, elastomers, pigments, paints and sizing materials. 1. A method for the fixation of metals , transition metals and their oxides on a siliceous support material of plant origin , characterized in that:a. silicate-containing biomass is used, wherein the latter contains more than 0.5% of silicates (relative to the dry mass of the biomass used),b. the spectrum of the non-silicon metals present in the biomass (this means all metals apart from silicon) is defined in that in a first washing step, all unwanted non-silicon metals present in the biomass are dissolved by means of the washing solution used and the washing solution is removed and in that in a second step, the biomass is treated with a substance or is soaked in the latter which contains the required metals and/or transition metals and/or their oxides or their mixtures,c. the metals and/or transition metals and/or their oxides or their mixtures present in the biomass are fixed in a combustion step on the siliceous skeleton of the plant, which remains at the end of combustion as ash, on which the existing metals and/or transition metals and/or their oxides or their mixtures have been fixed,d. pre-drying of the biomass may optionally be carried out before combustion.2. The method as claimed in claim 1 , characterized in that the steps for removing existing non-silicon metals by means of washing in a washing solution claim 1 , which dissolves existing non-silicon metals claim 1 , and removing the washing solution claim 1 , are omitted.3. The method as claimed in claim 1 , characterized in that the temperature in the combustion is controlled so that:a. no melts are ...

Methods of Preparing an Aromatization Catalyst

Catalysts and method of preparing the catalysts are disclosed. One of the catalysts includes a zeolite support, a Group VIII metal on the zeolite support, and at least two halides bound to the zeolite support, to the Group VIII metal, or to both, and can have an average crush strength greater than 11.25 lb based on at least two samples of pellets of the catalyst measured in accordance with ASTM D4179. 1. A catalyst comprising: a zeolite support; a Group VIII metal on the zeolite support; and at least two halides bound to the zeolite support , to the Group VIII metal , or to both;wherein an average crush strength of the catalyst is greater than 11.25 lb based on at least two samples of pellets of the catalyst measured in accordance with ASTM D4179.2. The catalyst of claim 1 , wherein each of the at least two samples of pellets has 50 pellets.3. The catalyst of claim 1 , wherein the average crush strength is greater than 12 lb based on at least two samples of pellets of the catalyst measured in accordance with ASTM D4179.4. The catalyst of claim 1 , wherein an average crush strength per length of the catalyst is greater than about 2.48 lb/mm.5. The catalyst of claim 4 , wherein the average crush strength per length of the catalyst is in a range of from about 3.00 lb/mm to about 3.10 lb/mm.6. The catalyst of claim 1 , wherein less than 22% of the pellets that are measured in accordance with ASTM D4179 have an individual pellet crush strength of less than 10 lb/pellet.7. The catalyst of claim 6 , wherein less than 21% of the pellets that are measured in accordance with ASTM D4179 have an individual pellet crush strength of less than 10 lb/pellet.8. The catalyst of claim 1 , wherein less than 14% of the pellets that are measured in accordance with ASTM D4179 have an individual pellet crush strength of less than 9 lb/pellet.9. The catalyst of claim 8 , wherein less than 13% of the pellets that are measured in accordance with ASTM D4179 have an individual pellet crush ...

HETERGENOUS CATALYSIS FOR THE ACETIC ACID PRODUCTION BY METHANOL CARBONYLATION

Disclosed is a heterogeneous catalyst for producing acetic acid by carbonylation of methanol. In the heterogeneous catalyst, a rhodium complex ion is ionically bonded to an insoluble catalyst support, and the insoluble catalyst support includes a fluoropolymer having a quaternary pyridine radical alone or in combination with an acetate radical grafted on the surface thereof. According to the disclosure, a fixed-bed bubble column reactor can be easily designed. In addition, a special device for catalyst separation is not required, and thus the device manufacturing cost can be saved, the operating cost can be reduced due to process simplification, and productivity can be greatly increased. 1. A heterogeneous catalyst for producing acetic acid by carbonylation of methanol , wherein a rhodium complex ion is ionically bonded to an insoluble catalyst support , and the insoluble catalyst support includes a fluoropolymer having a quaternary pyridine radical alone or in combination with an acetate radical grafted on a surface thereof.2. The heterogeneous catalyst of claim 1 , wherein grafting the pyridine radical as a ligand on the surface of the fluoropolymer is achieved by diluting vinylpyridine in a solvent to a concentration of 20 wt % to 70 wt % claim 1 , adding Mohr's salt as a polymerization inhibitor thereto claim 1 , and irradiating cobalt gamma rays.3. The heterogeneous catalyst of claim 1 , wherein grafting the pyridine radical and the acetate group as a ligand to the surface of the fluoropolymer is achieved by mixing more than 0 mol % but not more than 35 mol % of vinyl acetate with vinylpyridine to obtain a vinylpyridine/vinyl acetate mixture claim 1 , diluting the vinylpyridine/vinyl acetate mixture in a solvent to a concentration of 20 wt % to 70 wt % claim 1 , adding Mohr's salt as a polymerization inhibitor thereto claim 1 , and irradiating cobalt gamma rays.4. The heterogeneous catalyst of any one of claims 1 , wherein the fluoropolymer for grafting is any ...

Exhaust gas purifying catalyst and production process thereof

Disclosed is an exhaust gas purifying catalyst in which grain growth of a noble metal particle supported on a support is suppressed. Also disclosed is a production process for producing an exhaust gas purifying catalyst. The exhaust gas purifying catalyst comprises a crystalline metal oxide support and a noble metal particle supported on the support, wherein the noble metal particle is epitaxially grown on the support, and wherein the noble metal particle is dispersed and supported on the outer and inner surfaces of the support. The process for producing an exhaust gas purifying catalyst comprises masking, in a solution, at least a part of the surface of a crystalline metal oxide support by a masking agent, introducing the support into a noble metal-containing solution containing a noble metal, and drying and firing the support and the noble metal-containing solution to support the noble metal on the support.

Stable support for fischer-tropsch catalyst

A process has been developed for preparing a Fischer-Tropsch catalyst precursor and a Fischer-Tropsch catalyst made from the precursor. The process includes contacting a gamma alumina catalyst support material with a first solution containing a vanadium compound and a phosphorus compound, to obtain a modified catalyst support material. The modified catalyst support material is calcined at a temperature of at least 500° C. The modified catalyst support is less soluble in acid solutions than an equivalent unmodified catalyst support. The modified catalyst support loses no more than 6% of its pore volume when exposed to water vapor. The modified catalyst support is contacted with a second solution which includes a precursor compound of an active cobalt catalyst component to obtain a catalyst precursor. The Fischer-Tropsch catalyst has enhanced hydrothermal stability as measured by losing no more than 10% of its pore volume when exposed to water vapor.

Catalyst support materials and catalyst materials useful for fischer-tropsch processes

The present disclosure relates to catalyst support materials and cobalt catalyst materials including such support materials, and their uses in Fischer-Tropsch processes. In certain aspects, a catalyst support material includes alumina, silicon oxide and titanium dioxide. In other aspects, a catalyst material includes a catalyst support material as described herein, with a catalytic metal such as cobalt disposed thereon.

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 Å to about 500 Å. 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. 1. A process comprising: [{'b': '5', '(a) forming an aqueous slurry by combining at least one acidic compound and water in amounts sufficient to provide an initial aqueous slurry having a pH of less than ;'}, '(b) adding an amount of at least one alkaline compound to the initial aqueous slurry in an amount sufficient to provide a second slurry having a pH greater than 7 to precipitate seed alumina in the form of alumina-containing slurry;', 'steps (a) and (b) comprising a pH swing cycle;', '(c) repeating steps (a) to (b) at least 1 additional time or swing cycle to provide an alumina-containing slurry having pH greater than 7;', '(d) adding an acidic compound to the alumina containing slurry of step (c) in an amount sufficient to provide an alumina-containing slurry having a pH of less than 5;', '(e) adding an alkaline compound to the alumina-containing slurry of step (d) in an amount sufficient to provide a final alumina-containing slurry having a pH of at least about 9; and', '(f) recovering precipitated alumina from the final alumina-containing slurry;, '(I) contacting acidic and alkaline compounds capable of forming alumina by conducting pH swing cycles comprisingwherein the temperature during steps (a)-(e) is maintained at about 72° C. or less; and(II) forming a precipitated alumina ...

Semiconductor material based on metal nanowires and porous nitride and preparation method thereof

Provided are a semiconductor material based on metal nanowires and a porous nitride, and a preparation method thereof. The semiconductor material includes: a substrate; a buffer layer formed on the substrate; and a composite material layer formed on the buffer layer the composite material layer includes: a transverse porous nitride template layer; and a plurality of metal nanowires filled in pores of the transverse porous nitride template layer.

PROMOTED CARBIDE-BASED FISCHER-TROPSCH CATALYST, METHOD FOR ITS PREPARATION AND USES THEREOF

A precursor for a Fischer-Tropsch catalyst includes a catalyst support, cobalt or iron on the catalyst support and one or more noble metals on the catalyst support, wherein the cobalt or iron is at least partially in the form of its carbide in the as-prepared catalyst precursor, a method for preparing said precursor and the use of said precursor in a Fischer-Tropsch process. 1. A method of preparing a Fischer-Tropsch catalyst precursor comprising: a) at least one cobalt-containing precursor selected from cobalt benzoylacetonate, cobalt carbonate, cobalt cyanide, cobalt hydroxide, cobalt oxalate, cobalt oxide, cobalt nitrate, cobalt acetate, cobalt acetylacetonate, cobalt carbonyl or a mixture of two or more thereof;', 'b) one or more noble metal precursors; and', 'c) a polar organic compound;, 'depositing a solution or suspension comprisingonto a catalyst support, wherein the catalyst support comprises silica and the surface of the silica is coated with a non-silicon oxide refractory solid oxide; andcalcining the catalyst support onto which the solution or suspension has been deposited in an inert atmosphere.2. The method of claim 1 , further comprising drying the catalyst support onto which the solution or suspension has been deposited before the calcining.3. The method of claim 1 , wherein the solution or suspension contains no water.4. The method of claim 1 , wherein the inert atmosphere contains no oxygen.5. The method of claim 1 , wherein the polar organic compound comprises an organic amine claim 1 , organic carboxylic acid or salt thereof claim 1 , an ammonium salt claim 1 , alcohol claim 1 , phenoxide claim 1 , alkoxide claim 1 , amino acid claim 1 , compound containing a functional group such as one more hydroxyl claim 1 , amine claim 1 , amide claim 1 , carboxylic acid claim 1 , ester claim 1 , aldehyde claim 1 , ketone claim 1 , imine or imide groups claim 1 , a hydroxyamine claim 1 , trimethylamine claim 1 , triethylamine claim 1 , tetramethylamine ...

SELECTIVE SURFACE IMPREGNATION METHOD FOR CATALYTICALLY ACTIVE MATERIALS ON PARTICULATE CATALYST SUPPORT USING MUTUAL REPULSIVE FORCE AND SOBLUBILITY DIFFERENCE BETWEEN HYDROPHILIC SOLVENT AND HYDROPHOBIC SOLVENT

A method for preparing a catalyst having catalytically active materials selectively impregnated or supported only in the surface region of the catalyst particle using the mutual repulsive force of a hydrophobic solution and a hydrophilic solution and the solubility difference to a metal salt precursor between the hydrophobic and hydrophilic solutions. The hydrophobic solvent is a C2-C6 alcohol. The hydrophobic solvent is introduced into the catalyst support and then removed of a part of the pores connected to the outer part of the catalyst particle by drying under appropriate conditions. Then, a hydrophilic solution containing a metal salt is introduced to occupy the void spaces removed of the hydrophobic solvent, and the catalyst particle is dried at a low rate to selectively support or impregnate the catalytically active material or the precursor of the catalytically active material only in the outer part of the catalyst particle. 1. A selective surface supporting method for catalytically active materials using a repulsive force between a hydrophilic solvent and a hydrophobic solvent , the method comprising:{'b': '10', 'a catalyst support preparation step S of preparing a spherical or cylindrical porous inorganic oxide as a catalyst support;'}{'b': '100', 'a first immersion step S of immersing the catalyst support in a hydrophobic, first solvent to fill in surface pores and inner pores of the catalyst support with the hydrophobic, first solvent;'}{'b': '200', 'a first drying step S of performing a drying process to eliminate the hydrophobic, first solvent from the inner pores under the surface of the catalyst support, thus allowing the hydrophobic, first solvent to remain in the pores in an inner central region of the catalyst support;'}{'b': '300', 'a second immersion step S of dissolving catalytically active materials or a precursor of the catalytically active material in a hydrophilic, second solvent to prepare a hydrophilic solution and then immersing the ...

APPARATUS AND METHOD FOR PRODUCING CARBON NANOFIBERS FROM LIGHT HYDROCARBONS

A process and apparatus for producing carbon nanofibers. The process comprises two stages. The first stage involves oxidizing light hydrocarbon with carbon dioxide or water, or oxygen, or a combination thereof to a mixture of hydrogen and carbon monoxide. The second stage involves converting the produced hydrogen and the carbon monoxide to carbon nanofibers and steam. In this way, greenhouse gases may be reduced by using carbon dioxide and methane (and/or other light hydrocarbons) as reactants; and useful products may be produced, such as Carbon NanoFibers (CNF). 137.-. (canceled)38. A process for producing carbon nanofibers , the process comprising:in a first reactor, reacting a light hydrocarbon stream with an oxidizing agent to perform reforming reaction to produce an intermediate gas stream comprising hydrogen and carbon monoxide; andin a subsequent second reactor, converting the produced hydrogen and the carbon monoxide selectively to carbon nanofibers that build up inside the second reactor, and steam which exits the second reactor.39. The process of claim 38 , further comprising: separating claim 38 , using a separator claim 38 , the unreacted portions of COand the light hydrocarbon from the intermediate gas stream; and recycling the separated unreacted portions of COand the light hydrocarbon into the first reactor.40. The process of claim 39 , wherein the step of separating the unreacted portions of COand the hydrocarbon from the converted gas stream from the first reactor is carried out using a membrane separator.41. The process according to claim 38 , wherein the first reactor is configured to enable dry catalytic reforming of the hydrocarbon.42. The process according to claim 38 , wherein the process of conversion in the first reactor is carried out at a temperature between about 480° C. and about 850° C. claim 38 , and at a pressure up to about 5 MPa.43. The process according to claim 38 , wherein the hydrocarbon is methane.44. The process according to ...

METHODS OF PREPARING A CATALYST

A method of preparing a catalyst comprising a) contacting a non-aqueous solvent, a carboxylic acid, and a chromium-containing compound to form an acidic mixture; b) contacting a titanium-containing compound with the acidic mixture to form a titanium treatment solution; c) contacting a pre-formed silica-support comprising from about 0.1 wt. % to about 20 wt. % water with the titanium treatment solution to form a pre-catalyst; and d) thermally treating the pre-catalyst to form the catalyst. A method of preparing a catalyst comprising a) contacting a non-aqueous solvent and a carboxylic acid to form an acidic mixture; b) contacting a titanium-containing compound with the acidic mixture to form a titanium treatment solution; c) contacting a pre-formed chrominated silica-support comprising from about 0.1 wt. % to about 20 wt. % water with the titanium treatment solution to form a pre-catalyst; and d) thermally treating the pre-catalyst to form the catalyst. 1. A method of preparing a catalyst comprising:a) contacting a non-aqueous solvent and a carboxylic acid to form an acidic mixture wherein a volume ratio of non-aqueous solvent to carboxylic acid is from about 1:1 to about 100:1;b) forming a titanium treatment solution by contacting a titanium-containing compound with the acidic mixture of step a;c) contacting a pre-formed silica-support comprising from about 0.1 wt. % to about 20 wt. % water with the titanium treatment solution to form a titanated support;d) contacting the titanated support with a chromium-containing compound to form a pre-catalyst; ande) thermally treating the pre-catalyst to form the catalyst.2. The method of wherein the carboxylic acid comprises a Cto Ccarboxylic acid.3. The method of wherein the carboxylic acid comprises a Cto Ccarboxylic acid4. The method of wherein the carboxylic acid comprises a Cto Ccarboxylic acid.5. The method of wherein the carboxylic acid comprises formic acid claim 1 , acetic acid claim 1 , propionic acid claim 1 , or a ...

Composite Catalyst, Method for Manufacturing Composite Catalyst and Application Thereof

A composite catalyst includes a carrier and noble metal particles supported by the carrier, wherein the carrier is a nitrogen-doped porous carbon composite material having a plurality of passages. The nitrogen-doped porous carbon composite material can include a nitrogen-doped porous carbon material and a plurality of metal oxide particles. The plurality of metal oxide particles can be uniformly distributed in the nitrogen-doped porous carbon material. The plurality of metal oxide particles can be partially exposed through the plurality of passages. The noble metal particles can be tightly combined with the exposed metal oxide particles to achieve recombination. And the noble metal particles can be at least one of Pd metal particles, Pt metal particles, Ru metal particles, Rh metal particles, Ir metal particles, Au metal particles, or a combination thereof. 1. A method for manufacturing a composite catalyst comprising:dissolving a metal source in a solvent to obtain a premix;sequentially adding a nitrogen-containing biomass and a pore-forming agent to the premix, such that the metal source reacts with the pore-forming agent to obtain a mixture containing a metal precipitate, wherein the pore-forming agent is at least one of ammonium bicarbonate, ammonium carbonate, ammonium oxalate, ammonium hydrogen oxalate, oxalic acid, or a combination thereof, and a molar ratio of the metal source to the pore-forming agent is in a range of 1:1 to 1:20;treating the mixture by a first calcination at 500 degrees centigrade to 1200 degrees centigrade under an inert atmosphere to obtain a nitrogen-doped porous carbon composite material having a plurality of passages, wherein the nitrogen-doped porous carbon composite material comprises a nitrogen-doped porous carbon material and a plurality of metal oxide particles, the plurality of metal oxide particles are uniformly distributed in the nitrogen-doped porous carbon material, and a part of the plurality of metal oxide particles are ...

POLARIZED FIBER MATS FOR CATALYST SUPPORT STRUCTURES

A polymer-catalyst assembly includes polarized polymeric nanofibers retaining a plurality of catalytic metallic nanoparticles. A method of making the polarized polymer-catalyst assembly may include providing a fiber mat having polymeric nanofibers retaining a plurality of catalytic metallic nanoparticles, stretching the fiber mat in a uniaxial direction, simultaneous with the step of stretching, thermally heating the fiber mat, simultaneous with the steps of stretching and thermally heating, subjecting the fiber mat to an electric field, whereby the simultaneous steps of stretching, thermally heating, and subjecting thereby form a polarized fiber mat. 1. A polymer-catalyst assembly comprising polarized polymeric nanofibers retaining a plurality of catalytic metallic nanoparticles.2. The polymer-catalyst assembly of claim 1 , wherein the polarized polymeric nanofibers are made of a polymer selected from the group consisting of polyvinylidene fluoride (PVDF) claim 1 , poly(vinylidene fluoride-co-hexafluoropropylene) (PVDF-HFP) claim 1 , polymethyl methacrylate (PMMA) claim 1 , polyvinylchloride (PVC) claim 1 , polytetraflouroethylene (PTFE) claim 1 , polyethylene terephthalate (PET) claim 1 , polystyrene claim 1 , polyethylene claim 1 , polypropylene (PP) claim 1 , polycarbonate (PC) claim 1 , polysulfone (PS) claim 1 , and polyamides.3. The polymer-catalyst assembly of claim 1 , wherein the polarized polymeric nanofibers are made of polyvinylidene fluoride.4. The polymer-catalyst assembly of claim 1 , wherein the catalytic metallic nanoparticles are made of a metal selected from the group consisting of Ni claim 1 , Rh claim 1 , Ru claim 1 , Co claim 1 , Ir claim 1 , Pt claim 1 , Os claim 1 , Pd claim 1 , Au claim 1 , Pt claim 1 , Ti claim 1 , and Ir.5. The polymer-catalyst assembly of claim 1 , wherein the catalytic metallic nanoparticles are made of a metal oxide selected from the group consisting of oxides of Ni claim 1 , Rh claim 1 , Ru claim 1 , Co claim 1 , Ir ...

METHOD FOR HYDROGENATING AROMATICS USING A CATALYST OBTAINED BY IMPREGNATION COMPRISING A SPECIFIC SUPPORT

Process for hydrogenating at least one aromatic or polyaromatic compound contained in a hydrocarbon feedstock having a final boiling point of less than or equal to 650° C., said process being performed in the gas phase or in the liquid phase at a temperature of between 30 and 350° C., at a pressure of between 0.1 and 20 MPa, at a hydrogen/(aromatic compounds to be hydrogenated) mole ratio of between 0.1 and 10 and at an hourly space velocity (HSV) of between 0.05 and 50 h, in the presence of a catalyst comprising an active phase comprising nickel, said active phase not comprising any group VIB metal, and a support comprising an amorphous mesoporous alumina having a connectivity (Z) of greater than 2.7, the connectivity being determined from the nitrogen adsorption/desorption isotherms. 1. A process for hydrogenating at least one aromatic or polyaromatic compound contained in a hydrocarbon feedstock having a final boiling point of less than or equal to 650° C. , said process being performed in the gas phase or in the liquid phase , at a temperature of between 30 and 350° C. , at a pressure of between 0.1 and 20 MPa , at a hydrogen/(aromatic compounds to be hydrogenated) mole ratio of between 0.1 and 10 and at an hourly space velocity HSV of between 0.05 and 50 h , in the presence of a catalyst comprising an active phase comprising nickel , said active phase not comprising any group VIB metal , and a support comprising an amorphous mesoporous alumina having a connectivity (Z) of greater than 2.7 , the connectivity being determined from the nitrogen absorption/desorption isotherms.2. The process as claimed in claim 1 , in which the nickel content of said catalyst is between 5% and 65% by weight relative to the total weight of the catalyst.3. The process as claimed in claim 1 , in which said alumina support has a connectivity (Z) of between 2.7 and 10.4. The process as claimed in claim 1 , in which the support has a mesopore volume of greater than or equal to 0.40 mL/g. ...

Methods of Preparing an Aromatization Catalyst

Catalysts and method of preparing the catalysts are disclosed. One of the catalysts includes a zeolite support, a Group VIII metal on the zeolite support, and at least two halides bound to the zeolite support, to the Group VIII metal, or to both, and can have an average crush strength greater than 11.25 lb based on at least two samples of pellets of the catalyst measured in accordance with ASTM D4179.

BORON AND/OR CARBON NANOFIBER MODIFIED ALUMINA-SUPPORTED MOLYBDENUM-COBALT CATALYSTS USEFUL IN HYDRODESULFURIZATION

Carbon nanofiber doped alumina (Al-CNF) supported MoCo catalysts in hydrodesulfurization (HDS), and/or boron doping, e.g., up to 5 wt % of total catalyst weight, can improve catalytic efficiency. Al-CNF-supported MoCo catalysts, (Al-CNF-MoCo), can reduce the sulfur concentration in fuel, esp. liquid fuel, to below the required limit in a 6 h reaction time. Thus, Al-CNF-MoCo has a higher catalytic activity than Al—MoCo, which may be explained by higher mesoporous surface area and better dispersion of MoCo metals on the AlCNF support relative to alumina support. The BET surface area of Al—MoCo may be 75% less than Al-CNF-MoCo, e.g., 166 vs. 200 m/g. SEM images indicate that the catalyst nanoparticles can be evenly distributed on the surface of the CNF. The surface area of the AlMoCoB5% may be 206 m/g, which is higher than AlMoCoB0% and AlMoCoB2%, and AlMoCoB5% has the highest HDS activity, removing more than 98% sulfur and below allowed levels. 1. A hydrodesulfurization catalyst , comprising:catalytic material comprising molybdenum and cobalt; anda catalyst support comprising alumina;andwherein the catalyst support further comprises carbon nanofibers dispersed on a surface of the alumina; and/orwherein the catalyst further comprises a dopant comprising boron,wherein the catalytic material is homogenously dispersed on the catalyst support.2. The catalyst of claim 1 , wherein the catalyst support further comprises the carbon nanofibers.3. The catalyst of claim 1 , the dopant comprising the boron is present in a range of from 1 to 5.5 wt. % relative to total catalyst weight.4. The catalyst of claim 2 , the dopant comprising the boron is present.5. The catalyst of claim 1 , wherein the catalytic material comprises 12 to 18 wt. % of molybdenum claim 1 , relative to total catalyst weight.6. The catalyst of claim 1 , wherein the catalytic material comprises 3 to 8 wt. % of cobalt claim 1 , relative to total catalyst weight.7. The catalyst of claim 6 , wherein the catalytic ...

Catalyst system for producing ketones from epoxides

A catalyst composition is useful for producing a ketone from a compound containing at least one epoxide group, and the catalyst composition contains at least one precious metal; and at least one mixed oxide; wherein the mixed oxide contains zirconium dioxide and silicon dioxide; wherein the precious metal is supported and the support is not entirely made of the mixed oxide; and wherein a mass ratio of zirconium dioxide to silicon dioxide in the mixed oxide is 86:14 to 99.9:0.1.

CATALYST FOR CATALYTIC OXIDATIVE CRACKING OF HYDROGEN SULPHIDE WITH CONCURRENT HYDROGEN PRODUCTION

Disclosed is a catalyst suitable for the catalytic oxidative cracking of a HS-containing gas stream. The catalyst comprises at least one or more active metals selected from the group consisting of iron, cobalt, and nickel, supported by a carrier comprising ceria and alumina. The active metal is preferably in the form of its sulphide. Also disclosed is a method for the production of hydrogen from a HS-containing gas stream, comprising subjecting the gas stream to catalytic oxidative cracking so as to form Hand S, using a catalyst in accordance with any one of the composition claims. 1. A method for the production of hydrogen from a HS-containing gas stream , comprising subjecting the gas stream to catalytic oxidative cracking so as to form Hand S , using a catalyst comprising at least one active metal selected from the group consisting of iron , cobalt , nickel , and combinations thereof , wherein said active metal is supported by a carrier comprising ceria and alumina.2. The method of claim 1 , wherein the composition of the catalyst comprises nickel.3. The method of claim 1 , wherein the catalytic oxidative cracking is conducted with a molar ratio HS/Oin the feedstock higher than 2:1 claim 1 , preferably in the range of from 2:1 to 6:1.4. The method of claim 3 , wherein the ratio is in a range of from 3:1 to 5:1 claim 3 , preferably 3.5:1 to 4.5:1.5. The method of claim 1 , wherein the catalytic oxidative cracking is conducted using an oxygen-containing gas-stream comprising at least 40 vol. % oxygen claim 1 , preferably at least 60 vol. % oxygen.6. The method of claim 5 , wherein the oxygen-containing gas-stream is oxygen having a purity of from 90-100 vol. %. 7.7. The method of claim 1 , wherein the catalytic oxidative cracking is conducted at a temperature in a range from 700° C. to 1300° C. claim 1 , preferably in a range from 950° C. to 1250° C.8. The method of claim 1 , comprising a further step of subjecting formed SO claim 1 , and optionally also COS and/or ...

Preparation Process for Cu-based Catalyst and Use Thereof

The present invention relates to a preparation process for a Cu-based catalyst and use of the Cu-based catalyst as the dehydrogenation catalyst in producing a hydroxyketone compound such as acetoin. Said Cu-based catalyst shows a high the acetoin selectivity as the dehydrogenation catalyst for producing acetoin. 1. A process for preparing a Cu-based catalyst , which comprises the steps of:(1′) producing a catalyst precursor, wherein said catalyst precursor (calculated by weight and based on the total weight of said catalyst precursor) contains30-60% (preferably 40-50%) of Cu (as CuO),10-45% (preferably 30-45% or 35-45%) of at least one auxiliary metal selected from metal of Group IIA (preferably at least one of Mg, Ca, Ba and Sr), non-noble metal of Group VIII (preferably at least one of Fe, Co and Ni), metal of Group VIB (preferably Cr, Mo or W), metal of Group VIIB (preferably Mn or Re), metal of Group IIB (preferably Zn or Cd) and lanthanide metal (preferably at least one of Yb, La, Ce, Pr and Lu) of periodic table of elements (as oxide),optionally an alkali metal and0-30% (preferably 5-15%) of optionally a binder (preferably at least one inorganic binder selected from refractory oxide and aluminosilicate, more preferably at least one inorganic binder selected from alumina, bauxite, pseudo-boehmite, silica, silica-alumina, boehmite, attapulgite, bentonite, kaolin, diatomite and montmorillonite, more preferably at least one inorganic binder selected from alumina, silica, diatomite and kaolin, more preferably alumina) (on a dry basis and as oxide), and {'br': None, 'R1-C(═O)—R2\u2003\u2003(II)'}, '(2-2) contacting a mixture of a ketone represented by formula (II) (preferably at least one of acetoin, hydroxyacetone, 1-hydroxy-2-butanone and 4-hydroxy-2-butanone), a solvent (preferably at least one of C1-6 alcohols, more preferably at least one of C1-6 linear or branched monohydric alcohols, more preferably at least one of methanol and ethanol) and optionally an ...

FORMING NANOPARTICLES INTO POROUS STRUCTURES

Methods for making porous materials having metal alloy nanoparticles formed therein are described herein. By preparing a porous material and delivering the precursor solutions under vacuum, the metal precursors can be uniformly embedded within the pores of the porous material. Once absorption is complete, the porous material can be heated in the presence of one or more functional gases to reduce the metal precursors to metal alloy nanoparticles, and embed the metal alloy nanoparticles inside of the pores. As such, the metal alloy nanoparticles can be formed within the pores, while avoiding surface wetting and absorption problems which can occur with small pores. 1. A method for forming platinum alloy nanoparticles into porous carbon , comprising:heating a porous carbon material within a chamber, the porous carbon material having one or more pores;applying a vacuum to the chamber;impregnating the porous carbon material using a platinum precursor and a metal precursor;heating the precursor-impregnated porous carbon material to a functional temperature; anddelivering a functional gas to the precursor-impregnated porous carbon material, the platinum precursor and the metal precursors reacting with the functional gas to form platinum alloy nanoparticles within the one or more pores.2. The method of claim 1 , further comprising delivering a purge gas prior to heating the porous carbon material to the functional temperature claim 1 , the purge gas being a gas that is inert with respect to the platinum precursor solution and the metal precursor solution.3. The method of claim 1 , wherein the metal precursor comprises platinum claim 1 , copper claim 1 , nickel claim 1 , or combinations thereof.4. The method of claim 1 , wherein applying the vacuum creates a pressure within the chamber of less than 500 millibars.5. The method of claim 1 , wherein the porous carbon material is a mesoporous carbon.6. The method of claim 1 , wherein the functional gas is a gas mixture comprising ...

PROCESS FOR THE PREPARATION OF A CATALYST SUPPORT

Process for preparing a catalyst support which process comprises a) mixing pentasil zeolite having a bulk silica to alumina molar ratio in the range of from 20 to 150 with water, a silica source and an alkali metal salt, b) extruding the mixture obtained in step (a), c) drying and calcining the extrudates obtained in step (b), d) subjecting the calcined extrudates obtained in step (c) to ion exchange to reduce the alkali metal content, and e) drying the extrudates obtained in step (d); process for preparing a catalyst by furthermore impregnating such support with platinum in an amount in the range of from 0.001 to 0.1 wt % and tin in an amount in the range of from 0.01 to 0.5 wt %, each on the basis of total catalyst; ethylbenzene dealkylation catalyst obtainable thereby and a process for dealkylation of ethylbenzene which process comprises contacting feedstock containing ethylbenzene with such catalyst. 1. An ethylbenzene dealkylation catalyst , containing; a) mixing pentasil zeolite having a bulk silica to alumina molar ratio in the range of from 20 to 150 with water, a silica source and an alkali metal salt;', 'b) extruding the mixture obtained in step (a);', 'c) drying and calcining the extrudates obtained in step (b);', 'd) treating the extrudates obtained in step (c) with an aqueous solution of fluorosilicate salt to provide fluorosilicate-treated extrudates;', 'e) subjecting the fluorosilicate-treated extrudates obtained in step (d) to ion exchange with an aqueous ammonium containing solution to reduce the alkali metal content; and', 'f) drying the extrudates obtained in step (e); and, 'a support obtainable by a process which comprisesplatinum in an amount in the range of from 0.001 to 0.1 wt % and tin in an amount in the range of from 0.01 to 0.5 wt %, each on the basis of total catalyst.2. An ethylbenzene dealkylation catalyst as recited in claim 1 , wherein the silica source is selected from the group consisting of powder form silica claim 1 , silica sol ...

Filtration media for removing chloramine, chlorine and ammonia, and method of making the same

An activated carbon-based media for efficient removal of chloramines as well as chlorine and ammonia from an aqueous stream is presented, and a method for making the same. The method involves preparing activated carbon that remove chloramines efficiently from chloramine-rich aqueous media. In particular, this application relates to the use of high performance catalytically active carbon for an efficient removal of chloramine from drinking water in the form of a solid carbon block or granular carbon media. The activated carbon is treated with a nitrogen-rich compound, such as, melamine.

MULTI-METALLIC CATALYST DOPED WITH PHOSPHORUS AND YTTRIUM

The invention relates to a catalyst comprising a support, at least one noble metal M, tin, phosphorus and yttrium, the content of phosphorus element being less than or equal to 1% by weight, and the content of yttrium being less than or equal to 1% by weight relative to the mass of the catalyst. The invention also relates to the process for preparing the catalyst and to the use thereof in reforming. 1. Catalyst comprising:a support,at least one noble metal M, tin, phosphorus and yttrium,wherein the phosphorus content is between 0.3% and 1% by weight relative to the mass of the catalyst,and wherein the yttrium content is less than or equal to 1% by weight relative to the mass of the catalyst.2. The catalyst according to claim 1 , wherein the content of noble metal M is between 0.02% and 2% by weight relative to the mass of the catalyst.3. The catalyst according to claim 1 , wherein the metal M is platinum or palladium.4. The catalyst according to claim 1 , wherein the tin content is between 0.005% and 10% by weight relative to the mass of the catalyst.5. The catalyst according to claim 1 , wherein the yttrium content is between 0.01% and 0.5% by weight relative to the mass of the catalyst.6. The catalyst according to claim 1 , wherein the Sn/M atomic ratio is between 0.5 and 4.0 claim 1 , the P/M ratio is between 0.2 and 30.0 and the Y/M ratio is between 0.1 and 5.0.7. The catalyst according to claim 1 , wherein the support comprises silica claim 1 , alumina or silica-alumina.8. The catalyst according to claim 1 , wherein also contains a halogenated compound.9. The catalyst according to claim 8 , wherein the content of halogenated compound is between 0.1% and 8% by weight relative to the mass of the catalyst.1014-. (canceled) The present invention relates to the field of hydrocarbon conversion and more specifically to the reforming of hydrocarbon-based feedstocks in the presence of a catalyst to produce gasoline cuts and aromatic compounds. More particularly, the ...

CATALYST FOR 1,3-BUTADIENE PRODUCTION FROM ETHANOL

The present invention relates to a catalyst for the conversion of ethanol to 1,3-butadiene comprising a support, characterized in that silver (Ag) and copper (Cu) are present on the support in metal form, to a process for producing such a catalyst, to the use of such a catalyst for the conversion of ethanol to 1,3-butadiene, and to a process for the catalytic conversion of ethanol to 1,3-butadiene using such a catalyst. 1. A catalyst for the conversion of ethanol to 1 ,3-butadiene comprising:a support, characterized in that silver (Ag) and copper (Cu) are present on the support in metal form,the support comprising a first metal oxide, the first metal oxide of the support being silica anda second metal oxide, which is different from the first metal oxide, the second metal oxide being magnesium oxide.2. The catalyst according to claim 1 , wherein the silica of the support is silica fume.3. The catalyst according to claim 1 , wherein the magnesium oxide is nano-sized magnesium oxide.4. The catalyst according to claim 1 , wherein the weight ratio between the first metal oxide and the second metal oxide in the support is in the range of 100:1 to 1:100.5. The catalyst according to claim 1 , wherein the weight ratio between silver (Ag) and copper (Cu) on the support is in the range of 10:1 and 1:10.6. The catalyst according to claim 1 , wherein the particle size of the catalyst is between 1 and 100 μm claim 1 , measured by electron microscopy (SEM) according to ASTM standard E986:04.7. The catalyst according to claim 1 , wherein the combined weight (metal loading) of Ag and Cu present on the support is in the range of 1% and 30% claim 1 , based on the total weight of the catalyst claim 1 , measured by X-ray fluorescence (XRF) techniques according to ASTM standard D4326:04.8. The catalyst of claim 1 , wherein the surface area of the catalyst is in the range of 60 to 400 m/g claim 1 , measured by Brunauer-Emmett-Teller method (BET) according to ASTM standard D6556:10.9. The ...

Catalyst comprising a boron-doped active phase

A catalyst containing an active phase comprising at least one metal of group VIIIB selected from cobalt, nickel, ruthenium and iron deposited on a support containing silica, alumina and at least one simple spinel MAl2O4 or mixed spinel MxM′(1−x)Al2O4) which is or is not partial, wherein M and M′ are separate metals selected from the group formed by magnesium, copper, cobalt, nickel, tin, zinc, lithium, calcium, caesium, sodium, potassium, iron and manganese, and wherein x is between 0 and 1, the values 0 and 1 being themselves excluded, characterised in that said active phase further comprises boron, the boron content being between 0.001% and 0.5% by weight with respect to the total weight of the catalyst, the value 0.5 being itself excluded.

CATALYST AND SYSTEM FOR METHANE STEAM REFORMING BY RESISTANCE HEATING; SAID CATALYST'S PREPARATION

The invention relates to a structured catalyst for catalyzing steam methane reforming reaction in a given temperature range T upon bringing a hydrocarbon feed gas into contact with the structured catalyst. The structured catalyst comprises a macroscopic structure, which comprises an electrically conductive material and supports a ceramic coating. The macroscopic structure has been manufactured by 3D printing or extrusion and subsequent sintering, wherein the macroscopic structure and the ceramic coating have been sintered in an oxidizing atmosphere in order to form chemical bonds between the ceramic coating and the macroscopic structure. The ceramic coating supports catalytically active material arranged to catalyze the steam methane reforming reaction, wherein the macroscopic structure is arranged to conduct an electrical current to supply an energy flux to the steam methane reforming reaction. The invention moreover relates to methods of manufacturing the structured catalyst and a system using the structured catalyst. 1. A structured catalyst for catalyzing steam methane reforming reaction in a given temperature range T upon bringing a hydrocarbon feed gas into contact with said structured catalyst , said structured catalyst comprising a macroscopic structure , said macroscopic structure comprising an electrically conductive material , said macroscopic structure having a resistivity between 10Ω-m and 10Ω-m in the given temperature range T , and said macroscopic structure supporting a ceramic coating , wherein the macroscopic structure has been manufactured by extrusion or 3D printing and by subsequent sintering , wherein said macroscopic structure and said ceramic coating have been sintered in an oxidizing atmosphere in order to form chemical bonds between said ceramic coating and said macroscopic structure , wherein said ceramic coating supports catalytically active material , said catalytically active material being arranged to catalyze the steam methane ...

Catalyst for hydrogen combustion, process for producing same, and method for hydrogen combustion

The hydrogen combustion catalyst includes a catalyst metal supported on a carrier made of an inorganic oxide, wherein: a functional group having at least one alkyl group with three or less carbon atoms is bonded to a terminal of a hydroxyl group on the carrier surface by substitution; platinum and palladium are supported as the catalyst metal; and a chlorine content is 300 ppm to 2,000 ppm per 1 mass % of the total supported amount of a supported amount of platinum and a supported amount of palladium. The total supported amount of platinum and palladium is preferably 0.1 to 5.0 mass % based on mass of a whole catalyst. In the hydrogen combustion catalyst according to the present invention, when treating a gas that contains iodine and hydrogen, catalyst poisoning by iodine is suppressed.

NOBLE METAL ZEOLITE CATALYST FOR SECOND-STAGE HYDROCRACKING TO MAKE MIDDLE DISTILLATE

A second-stage hydrocracking catalyst is provided, comprising: a) a zeolite beta having an OD acidity of 20 to 400 μmol/g and an average domain size from 800 to 1500 nm2; b) a zeolite USY having an ASDI between 0.05 and 0.12; c) a catalyst support; and d) 0.1 to 10 wt % noble metal; wherein the second-stage hydrocracking catalyst provides a hydrogen consumption less than 350 SCFB across a range of synthetic conversions up to 37 wt % when used to hydrocrack hydrocarbonaceous feeds having an initial boiling point greater than 380° F. (193° C.). A second-stage hydrocracking process using the second-stage hydrocracking process is provided. A method to make the second-stage hydrocracking catalyst is also provided. 1. A second-stage hydrocracking process , comprising:hydrocracking a hydrocarbonaceous feed having an initial boiling point greater than 380° F. (193° C.) in a second-stage hydrocracking reactor using a second-stage hydrocracking catalyst, wherein greater than 70 wt % of an effluent from the second-stage hydrocracking reactor has a hydrocracked boiling point greater than 380° F. (193° C.) and wherein the second-stage hydrocracking catalyst provides a hydrogen consumption less than 350 SCFB across a range of synthetic conversions up to 37 wt %; wherein the second-stage hydrocracking catalyst comprises:{'sup': '2', 'a. a zeolite beta having an OD acidity of 20 to 400 μmol/g and an average domain size from 800 to 1500 nm;'}b. a zeolite USY having an ASDI between 0.05 and 0.12;c. a catalyst support; andd. 0.1 to 10 wt % noble metal.2. The process of claim 1 , wherein a wt % of the zeolite beta is greater than the wt % of the zeolite USY in the second-stage hydrocracking catalyst.3. The process of claim 1 , wherein the zeolite beta has the OD acidity from 30 to 100 μmol/g.4. The process of claim 1 , wherein the zeolite beta has the average domain size from 900 to 1250 nm.5. The process of claim 1 , wherein the zeolite USY has a total Bronsted acid sites determined ...

Cerium-based active materials with catalytic capacity and process for obtaining them

The present invention relates to combinations comprising hydrogen gas or a hydrogen donor agent and nanoclays comprising metallic cerium or cerium oxide particles. The invention also relates to compositions, nanocomposite materials and containers comprising these combinations. Additionally, the present invention relates to methods for obtaining these combinations and to the use thereof in packaging oxygen- and oxidation-sensitive products.

Supported Nanoparticle Compositions and Precursors, Processes for Making the Same and Syngas Conversion Processes

Disclosed are novel supported nanoparticle compositions, precursors, processes for making supported nanoparticle compositions, processes for making catalyst compositions, and processes for converting syngas. The catalyst composition can comprise nanoparticles comprising metal oxide(s), such as manganese cobalt oxide. This disclosure is particularly useful for converting syngas via the Fischer-Tropsch reactions to make olefins and/or alcohols. 1. A supported nanoparticle composition comprising:a support; anda plurality of nanoparticles on the support, wherein:each nanoparticle comprises a kernel, the kernels have an average particle size from 4 to 100 nm and a particle size distribution of no greater than 20%; the kernels comprise oxygen, a metal element M1, optionally sulfur, optionally phosphorus, an optional metal element M2, and optionally a third metal element M3, where:M1 is selected from Mn, Fe, Co, and combination of two or more thereof;M2 is selected from Ni, Zn, Cu, Mo, W, Ag, and combinations thereof;M3 is selected from Y, Sc, alkaline metals, the lanthanides, group 13, 14, or 15 elements, and combinations thereof; andthe molar ratios of M2, M3, S, and P, if any, to M1 is r1, r2, r3, and r4, respectively, 0≤r1≤2, 0≤r2≤2, 0≤r3≤5, and 0≤r4≤5.2. The supported nanoparticle composition of claim 1 , wherein 0.05≤r1≤0.5 claim 1 , and 0.005≤r2≤0.5.3. The supported nanoparticle composition of claim 1 , wherein the kernels comprise an oxide of at least one metal element from the M1 claim 1 , the M2 claim 1 , or the M3.4. The supported nanoparticle composition of claim 1 , wherein the nanoparticles have an average particle size of from 4 to 20 nm.5. The supported nanoparticle composition of claim 1 , wherein the nanoparticles have a particle size distribution of from 5 to 15%.6. The supported nanoparticle composition of claim 1 , wherein the kernels comprise at least two metal elements.7. The supported nanoparticle composition of claim 1 , wherein the nanoparticles ...

Heterogeneous catalyst and method for selectively hydrogenating copolymer

A heterogeneous catalyst for selectively hydrogenating a copolymer is provided, which includes a porous support, a metal oxide wrapping a part of the surface of the porous support, and a plurality of palladium particles on the porous support and the metal oxide. A method for selectively hydrogenating a copolymer is also provided, which includes contacting a heterogeneous catalyst to a copolymer to process hydrogenation. The copolymer includes aromatic rings and nonaromatic double bonds, and the nonaromatic double bonds are hydrogenated, and the aromatic rings are substantially not hydrogenated. The heterogeneous catalyst includes a porous support, a metal oxide wrapping a part of the surface of the porous support, and a plurality of palladium particles formed on the porous support and the metal oxide.

METHOD FOR PREPARING CATALYST FOR SELECTIVE HYDROGENATION OF DIOLEFINS

The present invention relates to a catalyst and a method for preparation of that catalyst for the selective hydrogenation of diolefins present in gasoline streams along with the shifting of lighter sulfur compounds in the feed stock to heavier sulfur compound by the reaction with olefinic compounds. 1. A catalyst for simultaneously carrying out selective hydrogenation of diolefins and conversion of light sulfur compounds to heavier sulfur compounds in the gasoline streams , wherein the catalyst comprises:at least one metal from group VIB and at least one metal from group VIII mounted on the surface of an alumina support, andthe catalyst having two types of metal active sites, wherein one active site of the catalyst comprising preferentially only group VIB metals and, another type of active site of the catalyst comprising a mixture of group VIB and group VIII metals,wherein the group VIB metals in the catalyst is in range of 5% to 15% by weight as metal oxide with respect to the total dry weight of the catalyst and the group VIII metal is in range of about 0.5% to 5% by weight as metal oxide with respect to the total dry weight of the catalyst.2. The catalyst as claimed in claim 1 , wherein the catalyst is having of pore volume at least 60% from the pores of diameter in the range 60-120 Å claim 1 , and pore volume in the range of 10 to 20% from the pores of diameter in the range >120 Å out of total pore volume of the catalyst.3. The catalyst as claimed in claim 1 , wherein the active site of the catalyst comprising group VIB metal is responsible for the combination reactions of lighter sulfur compound with olefins compounds and the active site of the catalyst comprising a mixture of group VIII and group VIB metals is responsible for selective hydrogenation of the diolefins.4. A method for preparation of a catalyst for simultaneously carrying out selective hydrogenation of diolefins in the gasoline streams and conversion of light sulfur compounds to heavier compounds ...

Method for producing catalyst, and method for producing unsaturated nitrile

The present invention provides a method for producing a catalyst to be used for a gas-phase catalytic ammoxidation reaction of propane, the method comprising a preparation step of dissolving or dispersing a raw material to thereby obtain a prepared raw material liquid, a first drying step of drying the prepared raw material liquid to thereby obtain a dried material, a calcination step of calcining the dried material to thereby obtain a composite oxide having a predetermined composition, an impregnation step of impregnating the composite oxide with a solution containing at least one specific element selected from the group consisting of tungsten, molybdenum, tellurium, niobium, vanadium, boron, bismuth, manganese, iron, antimony, phosphorus and rare earth elements to thereby obtain an impregnated composite oxide, and a second drying step of drying the impregnated composite oxide, wherein at least one of the impregnation step o and the second drying step is a step of impregnating the composite oxide or drying the impregnated composite oxide while stirring by a specific stirring power.

Sulfur-Tolerant CO Shift Conversion Catalyst and Preparation Method Thereof

The present invention discloses a sulfur tolerant carbon monoxide shift conversion catalyst, prepared by the following materials: magnesium source, aluminum source, oxide flux, crystal growth agent, rare earth additive, CoO, MoOand an acidic aqueous solution. A preparation method of the catalyst is provided, comprising the steps of: S1, Adding an aqueous acidic solution and a specific amount of rare earth additive to a specific amount of magnesium source, aluminum source, oxide flux and crystal growth agent, followed by kneading to produce a mixture; S2, Extruding the mixture to obtain an extruded strip product; S3, Drying the extruded strip product to give a semi-finished product; S4, Calcining the semi-finished product to obtain a catalyst carrier; S5, Impregnating the catalyst carrier with the active components CoO and MoOby an incipient-wetness impregnation method to obtain an impregnated product; and S6, Calcining the impregnated product to obtain the catalyst. The oxide flux and crystal growth agent can participate in a solid phase reaction between the magnesium source and aluminum source to form spinel structure, thereby improving the mechanical strength and stability of the spinel. The nano-sized active component can effectively improve the dispersion of the active component, and improve the catalytic activity of the granular boundary of the active component. 1. A sulfur tolerant CO shift conversion catalyst , at least prepared by the following materials: [{'sub': 2', '3, 'an aluminum source, a molar ratio of the magnesium source to the aluminum source is 0.92-1.36 wherein the magnesium source is calculated in the form of MgO and the aluminum source is calculated in the form of AlO;'}, 'an oxide flux, 1.5-3.0 parts by weight;', 'a crystal growth agent, 1.5-3.6 parts by weight;', 'a rare earth additive, 0.9-3.0 parts by weight;', 'CoO, 0.2-1.5 parts by weight;', {'sub': '3', 'MoO, 1.4-3.2 parts by weight; and'}, 'an acidic aqueous solution, 37.8-63.3 parts by ...

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 ...

CATALYST MIXTURE FOR THE TREATMENT OF WASTE GAS

A catalyst comprises a mixture of 95% vol. to 30% vol. of an activated carbon catalyst and from 5% vol. to 70% vol. of a filler material as well as a configuration of such a catalyst for the removal of SO, heavy metals and/or dioxins form waste gas and liquids. 1. A catalyst comprising a mixture of 95% vol. to 30% vol. of an activated carbon catalyst and from 5% vol. to 70% vol. of a filler material wherein said filler material comprises plastic , alumina , metal , ceramic materials or mixture thereof.2. The catalyst as claimed in claim 1 , wherein the mixture contains no other solid ingredients than the activated carbon catalyst and the filler material.3. The catalyst as claimed in any one of to claim 1 , wherein the activated carbon catalyst is chosen from carbon catalyst that have been submitted to a physical treatment chosen among the group consisting of a pyrolyzis at a temperature range between 600 and 900° C. in inert atmosphere and a treatment in an oxidized atmosphere at a temperature between 850 and 950° C. claim 1 , a chemical treatment chosen among the group consisting of impregnation with an acid claim 1 , a strong base or salts or a combination of both a physical and a chemical treatment.4. The catalyst as claimed in any one of the preceding claims claim 1 , wherein the filler material has a shape chosen among saddle shaped claim 1 , ring shaped claim 1 , ball shaped claim 1 , torus shaped claim 1 , prism shaped or irregular shaped.5. The catalyst as claimed in any one of the preceding claims wherein for the treatment of waste gas having a SOcontent of the gas is between 300 ppm and 200 claim 1 ,000 ppm.6. The catalyst as claimed in any one of the preceding claims wherein the mixture comprises between 30% vol. and 60% vol. of an activated carbon catalyst impregnated with sulfur claim 1 , between 30% vol. and 60% vol. of an activated carbon catalyst impregnated with iron and between 5% vol. and 40% vol. of a filler material.7. The catalyst as claimed in ...

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 ...

STRUCTURED CATALYST FOR METHANOL REFORMING, METHANOL REFORMING DEVICE, METHOD FOR PRODUCING STRUCTURED CATALYST FOR METHANOL REFORMING, AND METHOD FOR PRODUCING AT LEAST ONE OF OLEFIN OR AROMATIC HYDROCARBON

To provide a highly active structured catalyst for methanol reforming that suppresses the decline in catalytic function and has excellent catalytic function, and a methanol reforming device. A structured catalyst for methanol reforming, including: 1. A structured catalyst for methanol reforming , comprising:a support of a porous structure composed of a zeolite-type compound; anda catalytic substance present in the support,the support comprising channels communicating with each other,the catalytic substance being a solid acid and being present at least in the channels of the support,each of the channels comprises an enlarged pore portion, andthe catalytic substance is at least embedded in the enlarged pore portion.2. The structured catalyst for methanol reforming according to claim 1 , wherein the enlarged pore portion communicates with a plurality of pores constituting any one of a one-dimensional pore claim 1 , a two-dimensional pore claim 1 , and a three-dimensional pore.3. The structured catalyst for methanol reforming according to claim 1 , wherein the solid acid is made of nanoparticles claim 1 , and an average particle size of the nanoparticles is greater than an average inner diameter of the channels and is less than or equal to an inner diameter of the enlarged pore portion.4. The structured catalyst for methanol reforming according to claim 3 , wherein the average particle size of the nanoparticles is from 0.1 nm to 50 nm.5. The structured catalyst for methanol reforming according to claim 3 , wherein a ratio of the average particle size of the nanoparticles to the average inner diameter of the channels is from 0.06 to 500.6. The structured catalyst for methanol reforming according to claim 5 , wherein the ratio of the average particle size of the nanoparticles to the average inner diameter of the channels is from 0.1 to 36.7. The structured catalyst for methanol reforming according to claim 5 , wherein the ratio of the average particle size of the ...

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.

MESOPOROUS AND MACROPOROUS NICKEL-BASED CATALYST HAVING A MEDIAN MACROPORE DIAMETER OF GREATER THAN 200 NM AND ITS USE WITH REGARD TO HYDROGENATION

The invention relates to a supported catalyst that comprises an oxide substrate that is for the most part calcined aluminum and an active phase that comprises nickel, with the nickel content being between 5 and 65% by weight of said element in relation to the total mass of the catalyst, with said active phase not comprising a metal from group VIB, the nickel particles having a diameter that is less than or equal to 20 nm, said catalyst having a median mesopore diameter of between 8 nm and 25 nm, a median macropore diameter of greater than 200 nm, a mesopore volume that is measured by mercury porosimetry that is greater than or equal to 0.30 mL/g, and a total pore volume that is measured by mercury porosimetry that is greater than or equal to 0.34 mL/g. The invention also relates to the method for preparation of said catalyst and its use in a hydrogenation method. 1. Supported catalyst that comprises an oxide substrate that is for the most part calcined aluminum and an active phase that comprises nickel , with the nickel content being between 5 and 65% by weight of said element in relation to the total mass of the catalyst , with said active phase not comprising a metal from group VIB , the nickel particles having a diameter that is less than or equal to 20 nm , said catalyst having a median mesopore diameter of between 8 nm and 25 nm , a median macropore diameter that is greater than 200 nm , a mesopore volume that is measured by mercury porosimetry that is greater than or equal to 0.30 mL/g , and a total pore volume that is measured by mercury porosimetry that is greater than or equal to 0.34 mL/g.2. Catalyst according to claim 1 , in which the substrate has a pore volume that is contained in the pores with a diameter of between 100 and 700 nm that is less than 20% of the total pore volume of the substrate.3. Catalyst according to claim 2 , in which the substrate has a pore volume that is contained in the pores with a diameter of between 100 and 700 nm that is less ...

CATALYST MATERIALS, SYSTEMS, AND METHODS OF MAKING

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

COBALT CATALYST COMPRISING A SUPPORT WITH A MIXED OXIDE PHASE CONTAINING COBALT AND/OR NICKEL, PREPARED USING AN ESTER COMPOUND

The invention concerns a catalyst containing an active cobalt phase deposited on a support comprising alumina, silica or silica-alumina, said support containing a mixed oxide phase containing cobalt and/or nickel, said catalyst being prepared by introducing at least one organic compound comprising at least one ester function. The invention also concerns its use in the field of Fischer-Tropsch synthesis processes. 1. A catalyst containing an active cobalt phase deposited on a support comprising alumina , silica or silica-alumina , said support containing a mixed oxide phase containing cobalt and/or nickel , said catalyst having been prepared by a process comprising at least: 'then carrying out', 'a) a step for bringing a support comprising alumina, silica or silica-alumina into contact with at least one solution containing at least one precursor of cobalt and/or nickel, then drying and calcining at a temperature in the range 700° C. to 1200° C., in a manner such as to obtain a mixed oxide phase containing cobalt and/or nickel in the support,'}b) a step for bringing said support containing said mixed oxide phase into contact with at least one solution containing at least one precursor of cobalt, 'the steps b) and c) possibly being carried out separately, in any order, or simultaneously,', 'c) a step for bringing said support containing said mixed oxide phase into contact with at least one organic compound comprising at least one ester function,'}d) then carrying out a drying step at a temperature of less than 200° C.2. The catalyst as claimed in claim 1 , in which the mixed oxide phase content in the support is in the range 0.1% to 50% by weight with respect to the weight of the support.3. The catalyst as claimed in claim 1 , in which the mixed oxide phase comprises an aluminate with formula CoAlOor NiAlOin the case of a support based on alumina or silica-alumina.4. The catalyst as claimed in claim 1 , in which the mixed oxide phase comprises a silicate with formula ...

PROCEDURE TO PREPARE A SUPPORTED TRIMETALLIC CATALYST FOR PRODUCTION OF ULTRA LOW SULFUR DIESEL AND ITS APPLICATION

According to this invention, a Ni—Mo—W trimetallic catalyst supported on porous alumina is obtained that shows very high activity for hydrotreating (HDT) of gasoils, particularly deep hydrodesulfurization (HDS) and hydrodesnitrogenation (HDN) of straight run gasoil in conditions of moderate pressure. 1. A procedure to obtain a supported trimetallic catalytic formulation for the deep hydrodesulfurization of straight run gasoil and for the production of ultra low sulfur diesel (ULSD) , comprising the following steps:a) preparation of solution containing tungsten (solution a), b) preparation of solution containing molybdenum, nickel and phosphorus (solution b), c) preparation of solution containing nickel and EDTA (solution c), d) preparation of solution containing nickel, molybdenum and EDTA (solution d) and e) mixture of solutions (c) and (d); e) drying the catalytic support at a temperature of 100 to 120° C., for 3 to 6 hours, f) impregnation of the solution (a), ageing of the material for 10 to 15 hours, drying at a temperature of 100 to 120° C. for 3 to 5 hours, g) impregnation of the solution (b), ageing of the material for 8 to 10 hours, drying at a temperature of 100 to 120° C. for 4 to 6 hours, h) impregnation of the mixture of the solutions c+d, ageing of the material during 30-40 minutes, no longer aging time is allowed, and drying at a temperature of 60 to 200° C., for 4 to 15 hours, i) wetting of the catalyst with SRGO, j) sulfiding the impregnated catalyst.2. A procedure according to claim 1 , wherein the following solutions are prepared;a) aqueous solution containing a metal of group VIB as tungsten, from ammonium metatungstate in water, until obtaining a completely transparent and crystalline solution;b) acid solution containing a metal of group VIB, such as Mo and a metal of group VIIIB as Ni, dissolved in a phosphoric acid solution;c) solution containing a metal of group VIIIB as Ni, and an organic compound such as ethylenediaminetetraacetic acid ( ...

Preparation method of platinum/tin/metal/alumina catalyst for direct dehydrogenation of n-butane and method for producing c4 olefins using said catalyst

The provided is a method for preparing a platinum-tin-metal-alumina catalyst by comprising: as an active ingredient, platinum which has a high activity in a direct dehydrogenation reaction of n-butane, tin which can increase the catalyst stability by preventing carbon deposition; additionally metal for reducing the level of catalyst inactivation over the reaction time; and an alumina carrier for supporting said components. Further, provided is a method for producing a high value product, C 4 olefins from low cost n-butane by using the catalyst prepared by the method according to the present invention in a direct dehydrogenation reaction.

Vertically aligned mesoporous thin film, method of manufacturing the same, and catalytic application thereof

This invention relates to a vertically aligned mesoporous silicate film with site-selective metal deposition from a single polymeric precursor and to diverse catalytic applications thereof. There is an innovative approach of a single precursor to manufacture a vertically aligned mesoporous silicate thin film having high thermal and chemical resistance on a large-area silicon wafer (2 cm×3 cm). A precisely designed organic-inorganic block copolymer (BCP) polyethyleneoxide-ss-polyvinylcyclicsilazane (PEO-ss-PVCSZ) with a disulfide bridge that is chemically cleavable is newly synthesized as the single precursor for an oriented silicate nanoporous film, and using such a precursor, solvent annealing, self-assembling, block cleaving treatment, and then hydrolysis conversion of a polymer into a siliceous phase at room temperature are carried out, thus directly forming a mesostructure on the substrate.