КОМПОЗИЦИЯ КАТАЛИЗАТОРА, СОДЕРЖАЩЕГО СЕРЕБРО, СПОСОБ ПОЛУЧЕНИЯ КАТАЛИТИЧЕСКОЙ КОМПОЗИЦИИ И ИСПОЛЬЗОВАНИЕ КАТАЛИТИЧЕСКОЙ КОМПОЗИЦИИ ДЛЯ ЭПОКСИДИРОВАНИЯ ЭТИЛЕНА

Настоящее изобретение относится к каталитической композиции, пригодной для использования при эпоксидировании этилена, способу ее получения и способу эпоксидирования этилена в присутствии этой каталитической композиции. Описана каталитическая композиция, включающая носитель, имеющий поверхность, по меньшей мере 500 м2/кг, и осаждение на носителе: - металлическое серебро, - металл или компонент, содержащий рений, вольфрам, молибден или соединение, образующее нитрат или нитрит, и - металла IA группы или компонент, содержащий металл IA группы, имеющий атомный номер, по меньшей мере, 37, и дополнительно калий, причем величина выражения (QK/R)+QHIA лежит в интервале значений от 1,5 до 30 ммоль/кг, где QHIA и QK означают количество в ммоль/кг металла IA группы, имеющего атомный номер, по меньшей мере, 37, и калия, соответственно, содержащихся в каталитической композиции, отношение QHIA к QK составляет, по меньшей мере, 1:1, величина QK составляет, по меньшей мере, 0,01 ммоль/кг, R означает безразмерную ...

НАНЕСЕННЫЙ НА ДИОКСИД КРЕМНИЯ КАТАЛИЗАТОР

Изобретение относится к нанесенному на диоксид кремния катализатору, используемому для производства соответствующего ненасыщенного нитрила в реакции парофазного каталитического аммоксидирования пропана или изобутана. Данный катализатор содержит оксид металла, представленный следующей формулой (1):в которой X представляет собой, по меньшей мере, один или несколько элементов, выбранных из Sb и Те; Т представляет собой, по меньшей мере, один или несколько элементов, выбранных из Ti, W, Mn и Bi; Z представляет собой, по меньшей мере, один или несколько элементов, выбранных из La, Ce, Yb и Y; и а, b, c, d и e находятся в интервалах, составляющих 0,05≤a≤0,5, 0,01≤b≤0,5, 0,001≤c≤0,5, 0≤d≤1, и 0≤e≤1, соответственно, и n представляет собой значение, которое удовлетворяет требованиям атомной валентности. При этом у нанесенного на диоксид кремния катализатора средний размер пор составляет от 60 до 120 нм, суммарный объем пор составляет 0,15 см/г или более, удельная площадь поверхности составляет от ...

НОСИТЕЛЬ КАТАЛИЗАТОРА ЭПОКСИДИРОВАНИЯ, ЕГО ПОЛУЧЕНИЕ И ПРИМЕНЕНИЕ

Носитель имеет скорость солюбилизации натрия, определенную по количеству натрия, выделившемуся при погружении носителя в кипящую воду при соотношении кипящей воды и носителя 3:1 (мас./мас.), не более 5 мас.ч. на млн., из расчета на общую массу носителя, за 5 мин. При этом способ получения катализатора заключается в том, что упомянутую скорость солюбилизации натрия достигают методом, эффективным для перевода ионизируемых частиц, находящихся на поверхности носителя, в ионное состояние, и удалении, по меньшей мере, части этих частиц, или перевода ионизируемых частиц в нерастворимое состояние, или перевода ионизируемых частиц в стационарное состояние. Катализатор содержит упомянутый носитель, серебро и необязательно промотор. Катализатор получают путем пропитки, где активность водородных ионов в растворе снижена добавлением основания. Кроме того, заявлен способ каталитического эпоксидирования алкена кислородсодержащим газом. Заявленные носители с контролируемой скоростью солюбилизации обеспечивают ...

КАТАЛИЗАТОР ОКИСЛЕНИЯ С СЕДЛОВИДНЫМИ ФОРМОВАННЫМИ ИЗДЕЛИЯМИ-НОСИТЕЛЯМИ

Изобретение касается катализатора окисления акролеина до акриловой кислоты, способа его изготовления, его применения для каталитического окисления в газовой фазе акролеина до акриловой кислоты и к способу получения акриловой кислоты посредством окисления в газовой фазе акролеина молекулярным кислородом на неподвижном слое катализатора. Катализатор окисления включает по меньшей мере одно неорганическое оксидное или керамическое формованное изделие-носитель с площадью поверхности BET менее чем 0,5 м/г, причем нижняя граница площади поверхности BET составляет 0,01 м/г, в расчете на носитель, которое покрыто с образованием сплошной оболочки обладающим каталитической активностью мультиэлементным оксидом, соответствующим общей формуле (I)гдеXозначает W, Nb, Та, Cr и/или Се,Xозначает Cu, Ni, Со, Fe, Mn и/или Zn,Xозначает Sb и/или Bi,Xозначает один или несколько щелочных и/или щелочноземельных металлов и/или N,Xозначает Si, Al, Ti и/или Zr,а означает число в пределах от 1 до 6,b означает число ...

НОСИТЕЛЬ ДЛЯ КАТАЛИЗАТОРА ОЛЕФИНОКСИДА

Изобретение относится к носителям для катализатора, используемого для эпоксидирования. Описан носитель для катализатора эпоксидирования олефина, причем указанный носитель имеет объем пор от пор с диаметром менее 1 мкм менее 0,20 мл/г и объем пор от пор с диаметром более 5 мкм менее 0,20 мл/г, в котором, по меньшей мере, 40% объема пор состоит из пор, имеющих диаметр в интервале от 1 мкм до 5 мкм. Описан катализатор эпоксидирования олефина, который включает носитель и каталитически эффективное количество серебра на нем, причем указанный носитель имеет объем пор от пор с диаметром менее 1 мкм менее 0,20 мл/г и объем пор от пор с диаметром более 5 мкм менее 0,20 мл/г в, котором, по меньшей мере, 40% объема пор состоит из пор, имеющих диаметр в интервале от 1 мкм до 5 мкм. Описан катализатор эпоксидирования олефина, который включает носитель и каталитически эффективное количество серебра на нем, причем указанный носитель имеет общий объем пор от 0,2 мл/г до 0,6 мл/г, площадь поверхности от ...

КАТАЛИЗАТОР ФИШЕРА-ТРОПША

Изобретение относится к катализатору Фишера-Тропша, содержащему кобальт и цинк, к способу его получения и применению в способе Фишера-Тропша. Описан катализатор, содержащий совместно осажденные частицы кобальта и цинка, причем указанные частицы имеют среднеобъемный размер частиц менее 150 мкм и распределение частиц по размерам, при котором, по меньшей мере, 90% объема частиц катализатора имеет размер между 0,4 и 2,5-кратный по отношению к среднему размеру частиц, и где атомное соотношение цинка и кобальта находится в пределах от 40 до 0,1. Описан также способ получения катализатора, по которому кислотный раствор, содержащий ионы цинка и ионы кобальта при общей концентрации от 0,1 до 5 мол/литр, и щелочной и кислотный раствор подают в реактор, содержащий водную среду, где кислотный раствор и щелочной раствор контактируют в водной среде при значении рН 4-9, отклоняющемуся самое большое на ±0,2 рН-единицы от заданного значения, при перемешивании, частота которого обусловлена подводимой мощностью ...

ПРИМЕНЕНИЕ ТВЕРДЫХ ВЕЩЕСТВ НА ОСНОВЕ ФЕРРИТА ЦИНКА В СПОСОБЕ ГЛУБОКОГО ОБЕССЕРИВАНИЯ КИСЛОРОДСОДЕРЖАЩЕГО СЫРЬЯ

Изобретение относится к области катализа. Описан способ обессеривания сырья, содержащего кислородсодержащие соединения, углеводородсодержащие соединения и серосодержащие органические соединения, улавливанием серы на улавливающей массе, содержащей оксиды железа или оксиды цинка и более 20 мас.% феррита цинка, причем вышеупомянутый способ осуществляют в присутствии водорода при температуре, находящейся в интервале от 200°С до 400°С. Технический результат - увеличение эффективности процесса. 9 з.п. ф-лы, 2 пр.

СПОСОБ ПОЛУЧЕНИЯ ОЛЕФИНОКСИДА, СПОСОБ ПРИМЕНЕНИЯ ОЛЕФИНОКСИДА И КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ

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

СПОСОБ АММИАЧНОГО ОКИСЛЕНИЯ АЛКАНОВ

Использование: в производстве синтетического волокна. Сущность изобретения: усовершенствованный способ аммиачного окисления алканов. Реагент 1: алкан. Реагент 2: NH3, О2. Условия реакции: паровая фаза, температура 350 - 550oС, общее давление 1 - 6 бар, объемная скорость газовой смеси 100 - 36000 ч-1 , в присутствии инертного газового разбавителя и твердого катализатора, активная фаза которого содержит, по меньшей мере, один элемент, но не более двух, выбираемый из группы, состоящей из Mg, Ca, Mn, Fe, U, La, Co. 11 з. п. ф-лы, 2 ил., 19 табл.

КАТАЛИЗАТОРЫ ДЛЯ ПОЛУЧЕНИЯ АЛКИЛЕНОКСИДОВ, ИМЕЮЩИЕ УЛУЧШЕНУЮ СТАБИЛЬНОСТЬ, ЭФФЕКТИВНОСТЬ И/ИЛИ АКТИВНОСТЬ

... 1. Катализатор для получения алкиленоксида с помощью эпоксидирования алкена в паровой фазе, содержащий нанесенное пропиткой серебро и, по меньшей мере, один промотор для увеличения эффективности на жаропрочный твердый носитель, и указанный носитель содержит количество компонента циркония, достаточное для улучшения, по меньшей мере, одного свойства из активности, эффективности и стабильности катализатора, по сравнению со сходным катализатором, который не содержит компонента циркония, указанный компонент циркония присутствует в носителе по существу в виде силиката циркония. 2. Катализатор по п.1, в котором количество нанесенного пропиткой серебра составляет примерно от 2 до 60% от массы катализатора. 3. Катализатор по п.2, в котором количество нанесенного пропиткой серебра составляет примерно от 5 до 50% от массы катализатора. 4. Катализатор по п.3, в котором количество нанесенного пропиткой серебра составляет примерно от 10 до 40% от массы катализатора. 5. Катализатор по п.1, в котором, ...

КАТАЛИЗАТОР ДЕГИДРИРОВАНИЯ, СПОСОБ ЕГО ПРИГОТОВЛЕНИЯ И МЕТОД ЕГО ИСПОЛЬЗОВАНИЯ

... 1. Способ получения катализатора дегидрирования, включающий промывку регенерата оксида железа, добавление по меньшей мере одного дополнительного катализаторного компонента для получения смеси и прокаливание смеси, где регенерат оксида железа не нагревают до температуры выше 350°С, пока не будет добавлен по меньшей мере один дополнительный катализаторный компонент. ! 2. Способ по п.1, в котором регенерат оксида железа перед промывкой имеет содержание хлорида по меньшей мере 700 мас.ч./млн относительно массы оксида железа в расчете на Fe2O3. ! 3. Способ по п.1 или 2, в котором промытый регенерат оксида железа имеет содержание хлорида самое большее 300 мас.ч./млн относительно массы оксида железа в расчете на Fe2O3. ! 4. Способ по п.1, в котором промытый регенерат оксида железа получают промывкой регенерата оксида железа водой. ! 5. Способ по п.1, в котором промытый регенерат оксида железа получают промывкой регенерата оксида железа кислотным раствором. ! 6. Способ по п.5, в котором кислотный ...

СПОСОБ ПОЛУЧЕНИЯ ПОРОШКА ПРОВОДЯЩЕГО СОЕДИНЕНИЯ ТИПА МАЙЕНИТА

... 1. Способ получения соединения типа майенита, способ включает(1) стадию формирования порошка - предшественника соединения типа майенита посредством воздействия на смесь порошка исходных материалов соединения типа майенита и воды гидротермальной обработки;(2) стадию формирования порошка соединения типа майенита посредством дегидратирования порошка предшественника посредством нагрева,(3) стадию формирования порошка активированного соединения типа майенита посредством нагрева порошка соединения типа майенита в атмосфере инертного газа или в вакууме в диапазоне температур от 400˚C до 1000˚C в течение трех часов или больше и(4) стадию инжекции электронов в соединение типа майенита посредством смешивания порошка активированного соединения типа майенита с восстанавливающим агентом и нагрева полученной в результате смеси в диапазоне температур от 400˚C до 1100˚C для осуществления восстановительной обработки, где получают порошок проводящего соединения типа майенита, имеющий концентрацию электронов ...

КАТАЛИЗАТОР ФИШЕРА-ТРОПША, ВКЛЮЧАЮЩИЙ ОКСИД КОБАЛЬТА И ЦИНКА

... 1. Катализатор, подходящий для катализирования реакции Фишера-Тропша, включающий металлический кобальт, нанесенный на оксид цинка и имеющий следующее распределение размера частиц по объему: ! <10% имеет размер частиц ниже 1 мкм, ! 70-99% имеет размер частиц между 1 и 5 мкм, и ! <20% имеет размер частиц выше 5 мкм. ! 2. Катализатор по п.1, имеющий следующее распределение размера частиц по объему: ! <10% имеет размер частиц ниже 1 мкм, ! 75-95% имеет размер частиц между 1 и 5 мкм, и ! <15% имеет размер частиц выше 5 мкм. ! 3. Катализатор по п.1 или 2, в котором средняя объемная величина частиц составляет менее чем 25 мкм, предпочтительно от 1,5 до 15 мкм. ! 4. Катализатор по п.1 или 2, в котором объем пор главным образом образован порами, имеющими диаметр в диапазоне 5-100 нм. ! 5. Катализатор по п.1 или 2, в котором объем пор составляет менее чем 0,5 мл/г, предпочтительно менее чем 0,45 мл/г. ! 6. Катализатор по п.1 или 2, в котором удельная поверхность составляет менее чем 120 м2/г, предпочтительно ...

СПОСОБ ПОЛУЧЕНИЯ ХИМИЧЕСКОГО ПРОИЗВОДНОГО ОКИСИ ОЛЕФИНА И РЕАКТОР, ПРИГОДНЫЙ ДЛЯ ТАКОГО СПОСОБА

... 1. Способ получения 1,2-диола, при этом способ включает ! взаимодействие сырья, содержащего олефин и кислород в присутствии катализатора эпоксидирования, находящегося в первом отделе одного или более рабочих микроканалов микроканального реактора с образованием окиси олефина, ! превращение окиси олефина с помощью диоксида углерода с образованием 1,2-карбоната во втором отделе одного или более рабочих микроканалов, расположенном ниже первого отдела, и ! превращение 1,2-карбоната с помощью воды или спирта с образованием 1,2-диола в третьем отделе одного или более рабочих микроканалов, расположенном ниже второго отдела. ! 2. Способ по п.1, где катализатор эпоксидирования включает металл 11 группы в количестве от 50 до 500 г/кг относительно массы катализатора. ! 3. Способ по п.1 или 2, где катализатор эпоксидирования содержит серебро, нанесенное на материал носителя. ! 4. Способ по п.3, где катализатор содержит, в качестве промотора(ов), один или более элементов, выбранных из рения, вольфрама ...

СПОСОБ ПОЛУЧЕНИЯ ОКИСИ ОЛЕФИНА ИЛИ ХИМИЧЕСКОГО ПРОИЗВОДНОГО ОКИСИ ОЛЕФИНА И РЕАКТОР, ПРИГОДНЫЙ ДЛЯ ТАКОГО СПОСОБА

... 1. Способ эпоксидирования олефина, при этом способ включает ! взаимодействие сырья, содержащего олефин и кислород, в присутствии катализатора эпоксидирования, находящегося в первом отделе одного или более рабочих микроканалов микроканального реактора с образованием посредством этого смеси, включающей окись олефина, и ! быстрое охлаждение окиси олефина во втором отделе одного или более рабочих микроканалов, находящемся ниже первого отдела, посредством теплообмена с теплообменной жидкостью. ! 2. Способ по п.1, где катализатор эпоксидирования включает металл 11 группы в количестве от 50 до 500 г/кг относительно массы катализатора. ! 3. Способ по п.1, где катализатор эпоксидирования содержит серебро, нанесенное на материал носителя. ! 4. Способ по п.3, где катализатор содержит в качестве промотирующего компонента(ов) один или более элементов, выбранных из рения, вольфрама, молибдена, хрома и их смесей, и, кроме того, один или более щелочных металлов, выбранных из лития, калия и цезия. ! 5.

ПРИМЕНЕНИЕ ИСТОЧНИКА ХРОМА В СОЧЕТАНИИ С ОСАЖДЕННЫМ КАТАЛИЗАТОРОМ В РЕАКЦИИ ФИШЕРА-ТРОПША

... 1. Применение источника хрома в сочетании с осажденным железным катализатором в высокотемпературном процессе Фишера-Тропша с целью преобразования реагентов в виде СО и Н2 в продукты реакции в виде углеводородов и возможно их оксигенатов путем введения в контакт СО и H2 с источником хрома в сочетании с осажденным железным катализатором в ходе двухфазной высокотемпературной реакции Фишера-Тропша, которую осуществляют в реакторе с псевдоожиженным слоем, при этом реагенты и продукты реакции находятся в газообразной фазе, а катализатор в твердой фазе. 2. Применение по п.1 для достижения, по меньшей мере, одного результата, выбранного из группы, включающей снижение концентрации органической кислоты в углеводородах и их оксигенатах, образующихся в результате процесса Фишера-Тропша, повышение активности осажденного железного катализатора с целью преобразования СО и H2 в углеводороды и возможно в их оксигенаты, снижение концентрации метана, образующегося в результате процесса Фишера-Тропша, уменьшение ...

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 ...

КОРКОВЫЙ КАТАЛИЗАТОР, ПРЕДНАЗНАЧЕННЫЙ, В ЧАСТНОСТИ, ДЛЯ ОКИСЛЕНИЯ МЕТАНОЛА В ФОРМАЛЬДЕГИД, И СПОСОБ ЕГО ИЗГОТОВЛЕНИЯ

... 1. Корковый катализатор, в частности, для окисления метанола в формальдегид, и содержащий на инертном, предпочтительно по существу непористом носителе по меньшей мере один слой покрытия, которое перед удалением органических составляющих компонентов b) и c) содержит ! a) оксиды или переводимые в соответствующие оксиды предшествующие соединения молибдена и железа, причем молярное соотношение Mo:Fe находится в интервале от 1:1 до 5:1, а также, в случае необходимости, другие металлические или металлооксидные составляющие или переводимые в соответствующие оксиды предшествующие соединения; ! b) по меньшей мере одно органическое связующее вещество; ! c) по меньшей мере один другой компонент, выбранный из группы, состоящей из золя SiO2 или его предшественника, золя Al2O3 или его предшественника, золя ZrO2 или его предшественника, золя TiO2 или его предшественника, жидкого стекла, MgO, цемента, мономеров, олигомеров или полимеров силанов, алкоксисиланов, арилоксисиланов, акрилоксисиланов, аминосиланов ...

НОСИТЕЛЬ КАТАЛИЗАТОРА, КАТАЛИЗАТОР И ЕГО ПРИМЕНЕНИЕ

... 1. Носитель катализатора, содержащий по меньшей мере 85 масс. процентов альфа-оксида алюминия, по меньшей мере 0,06 мас.% SiOи не более 0,04 мас.% NaO, обладающий водопоглощением не более 0,35 грамм воды/грамм носителя и отношением водопоглощения (грамм воды/грамм носителя) к площади поверхности (мносителя/грамм носителя) не более 0,50 грамм воды/мносителя.2. Носитель по п. 1, отличающийся тем, что содержание SiOне превышает 0,40 мас.%.3. Носитель по п. 1, отличающийся тем, что содержание SiOне превышает 0,30 мас.%.4. Носитель по п. 1, отличающийся тем, что содержание NaO не превышает 0,03 мас.%.5. Носитель по п. 1, отличающийся тем, что содержит по меньшей мере 0,15 мас.% SiO.6. Носитель по п. 1, отличающийся тем, что указанное отношение не превышает 0,45 г/м.7. Носитель по п. 1, отличающийся тем, что указанное отношение не превышает 0,40 г/м.8. Носитель по п. 1, отличающийся тем, что указанное водопоглощение не превышает 0,30 г/г.9. Носитель по п. 8, отличающийся тем, что указанная площадь ...

КАТАЛИЗАТОР ДЕГИДРОВАНИЯ УГЛЕВОДОРОДОВ

КАТАЛИЗАТОР, ГАЗОГЕНЕРАТОР И ТОЛКАТЕЛЬ С УЛУЧШЕННОЙ ТЕРМИЧЕСКОЙ СПОСОБНОСТЬЮ И КОРРОЗИОННОЙ СТОЙКОСТЬЮ

... 1. Катализатор, содержащий:носитель, содержащий оксид гафния и вплоть до равной части оксид циркония по массе, причем объединенные оксид гафния и оксид циркония, когда присутствуют, составляют, по меньшей мере, 50% масс. носителя, иактивный металл на поверхности данного носителя.2. Катализатор по п. 1, в котором данный активный металл содержит один металл из, по меньшей мере, родия, рутения, палладия, осмия, иридия или платины.3. Катализатор по п. 1, в котором данный носитель представляет собой оксид гафния на, по меньшей мере, 99% масс.4. Катализатор по п. 1, в котором данный носитель дополнительно содержит стабилизатор.5. Катализатор по п. 4, в котором данный стабилизатор содержит материал, выбранный из группы, содержащей оксид церия и оксид иттрия или любую их комбинацию.6. Катализатор по п. 1, в котором данный носитель имеет теоретическую плотность больше, чем 50%.7. Катализатор по п. 1, в котором данный активный металл составляет от 0,1% масс. до 50% масс. в расчете на полную массу ...

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИТИЧЕСКИ АКТИВНОЙ МАССЫ В ВИДЕ СМЕСИ СОДЕРЖАЩЕГО МОЛИБДЕН И ВАНАДИЙ МНОГОЭЛЕМЕНТНОГО ОКСИДА ПО МЕНЬШЕЙ МЕРЕ С ОДНИМ ОКСИДОМ МОЛИБДЕНА

ПОЛИМЕТАЛЛИЧЕСКИЕ ОКСИДНЫЕ МАССЫ, СОДЕРЖАЩИЕ МОЛИБДЕН, ВИСМУТ И ЖЕЛЕЗО

... 1. Содержащие молибден (Mo), висмут (Bi) и железо (Fe) полиметаллические оксидные массы общей стехиометрии Iв которой переменные имеют следующие значения:a = от 0,5 до 1;b = от 7 до 8,5;c = от 1,5 до 3,0;d = от 0 до 0,15;e = от 0 до 2,5 иx - это число, определяемое валентностью и численностью отличных от кислорода элементов в формуле I.и выполняют следующие условия:Условие 1: 12-b-1,5·c=A и 0,5≤A≤1,5;Условие 2: 0,2≤a/A≤1,3 иУсловие 3: 2,5≤b/c≤9.2. Полиметаллическая оксидная масса по п. 1, стехиометрический коэффициент d которой составляет от 0,04 до 0,1.3. Полиметаллическая оксидная масса по п. 1, стехиометрический коэффициент е которой составляет от 0,5 до 2.4. Полиметаллическая оксидная масса по п. 1, которая удовлетворяет условию 1: 0,5≤A≤1,25.5. Полиметаллическая оксидная масса по п. 1, которая удовлетворяет условию 2: 0,3≤a/A≤1,2.6. Полиметаллическая оксидная масса по одному из п.п. 1-5, которая удовлетворяет условию 3: 3≤b/c≤9.7. Оболочечный катализатор, включающий в себя формованное ...

СПОСОБ УГЛЕКИСЛОТНОГО РИФОРМИНГА УГЛЕВОДОРОДОВ ПРИ ВЫСОКОМ ДАВЛЕНИИ В ПРИСУТСТВИИ СОДЕРЖАЩИХ ИРИДИЙ

... 1. Катализатор углекислотного риформинга углеводородов, активная масса которого включает содержащий иридий активный компонент и содержащий диоксид циркония материал подложки, причем:a) содержание иридия в пересчете на содержание активной массы составляет от 0,01 до 10 мас.%, предпочтительно от 0,05 до 5 мас.%, более предпочтительно от 0,1 до 1 мас.%, иb) преимущественная часть диоксида циркония в содержащем диоксид циркония материале подложки обладает кубической и/или тетрагональной структурой, причем доля кубической и/или тетрагональной фазы составляет >50 мас.%, предпочтительно >70 мас.%, в особенности предпочтительно >90 мас.%2. Катализатор по п. 1, отличающийся тем, что содержащая диоксид циркония подложка включает дополнительные ингредиенты, причем доля тетрагонального и/или кубического диоксида циркония в пересчете на общую массу подложки составляет >80 мас.%, предпочтительно >90 мас.%, более предпочтительно >95 мас.%.3. Катализатор по п. 1 или 2, отличающийся тем, что содержащая ...

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 ...

Katalysator

Die vorliegende Erfindung betrifft einen beschichteten keramischen Katalysator, der in der Beschichtung und im Träger katalytisch aktive Komponenten enthält.

Zusammensetzung auf der Grundlage von Zirconiumoxid und von Oxiden von Cer, Lanthan und einer anderen seltenen Erde, Verfahren zur Herstellung derselben und Verwendung derselben als Katalysator

Preparing supported catalyst useful for decomposition of substances e.g. ozone, comprises providing carrier comprising polymer, dissolving carrier surface using solvent, applying catalyst to dissolved carrier surface, and removing solvent

Preparing a supported catalyst comprises: providing a carrier comprising a polymer, dissolving the surface of the carrier with an appropriate solvent, applying a catalyst to the partially dissolved surface of the carrier, and removing the solvent; or providing a carrier comprising a polymer, providing a suspension of a catalyst and a solvent, which can dissolve surface of the carrier, immersing the carrier in the suspension, and removing the solvent. Preparing a supported catalyst comprises: providing a carrier comprising a polymer, dissolving the surface of the carrier with an appropriate solvent, applying a catalyst to the partially dissolved surface of the carrier, and removing the solvent; providing a carrier comprising a polymer, providing a suspension of a catalyst and a solvent, which can dissolve surface of the carrier, immersing the carrier in the suspension, and removing the solvent; providing a carrier comprising a polymer, applying an adhesive coating to the surface of the carrier ...

Monomodale und polymodale Katalysatorträger und Katalysatoren mit engen Porengrößenverteilungen und deren Herstellverfahren

A process for the preparation of a chemical derivable from an olefin oxide, and a reactor suitable for such a process

A process for the preparation of an olefin oxide or a chemical derivable from an olefin oxide

PROCESS FOR THE PRODUCTION OF UNSATURATED ACIDS FROM CORRES PINDING UNSATURATED ALDEHYDES

... 1419671 Unsaturated carboxylic acids MITSUBISHI PETROCHEMICAL CO Ltd 7 Sept 1973 [7 Sept 1972 5 Dec 1972 5 July 1973] 42093/73 Heading C2C [Also in Division B1] Unsaturated acids, e.g. acrylic and methacrylic acids, are made by the vapour phase oxidation of an unsaturated aldehyde at 200- 400‹ C. in the presence of a catalyst of the formula Mo 12 V 0À1-10 Fe 0À1-6 Si a X b O 36-126 , wherein a = 0-24, b = 0-3À0, a + b = 0À1-27 and X is Na, K, Rb, Zn, Al, In, Tl, Ti, Zr, Ge, Nb, Ta, Cr, Mn, Co and/or Ni, which catalyst may be supported. The reaction may be at 0À5-10 atm. using 0À2-3 moles O 2 per mole aldehyde, optionally in the presence of steam.

CATALYTIC COMPOSITION

... 1332986 Catalytic composition BP CHEMICALS INTERNATIONAL Ltd 29 March 1972 [15 April 1971] 9470/71 Heading C1A [Also in Division C2] A catalytic composition containing cobalt, molybdenum and oxygen is prepared by precipitation from a solution or suspension having a pH less than 7 and containing molybdic acid or a molybdate of a nitrogenous base by the addition of a cobalt salt and a buffering agent, formed from an acid and a nitrogenous base, the resulting mixture having a pH of less than 7 and drying the precipitate. The buffering agent may be formed from a nitrogenous base and acetic, citric, phthalic, hydrochloric or nitric acids and the nitrogenous base can be one of ammonia, an aliphatic, aromatic, heterocyclic or cyclo aliphatic amine or hydrazine. The cobalt salt is preferably the nitrate chloride or acetate and the heat treatment consists of a two-stage heating, with intermediate pelletizing, first at 350-650‹ C. and then at 500-650‹ C.

Fischer-tropsch catalyst with low surface area alumina, its preparation and use thereof

Exhaust system for a compression ignition engine having a capture region for volatilised platinum

CATALYST AND PROCESS FOR THE PRODUCTION OF AMINES BY THE CATALYTIC HYDROGENATION OF NITRILES

... 1,214,035. Production of amines. CHEMISCHE WERKE HULS A.G. 26 April, 1968 [28 April, 1967], No. 19819/68. Heading C2C. [Also in Division B1] Amines are prepared by the catalytic hydrogenation of the corresponding nitriles in the presence of a cobalt catalyst precipitated on a carrier of coarsely pored -Al 2 O 3 having a crystalline fraction of -Al 2 O 3 of more than 70% by weight, a specific surface area of 0À5- 30 sq. m./g. and a water absorption of 30- 60 cc./100 g. The catalyst may contain 5-35% by weight of cobalt and also 0À05-12% by weight of one or more other metals e.g. Cr, Mn, Ni or Ag. The reaction is preferably carried out in the presence of NH 3 and an inert diluent, such as toluene or methanol, at 80-120‹ C. at superatmospheric pressure. In the examples adiponitrile is converted to hexamethylenediamine using a Co(Mn/Ag catalyst on an -Al 2 O 3 base and 1,2-bis-(#-cyanoethoxy) ethane is converted to 1,2-bis-(-aminopropoxy)ethane using the same catalyst.

Catalyst

CATALYTIC PROCESS FOR THE CONVERSION OF A SYNTHESIS GAS TO HYDROCARBONS

Catalytic process for the conversion of a synthesis gas to hydrocarbons

Catalytic process for the conversion of a synthesis gas to hydrocarbons

Catalytic process for the conversion of a synthesis gas to hydrocarbons

THREE ONE AND/OR VIERSCHICHTIGE OF CATALYST SYSTEMS FOR THE PRODUCTION OF PHTHALSÄUREANHYDRID

VERWENDUNG VON KRISTALLINEM ALFA-ALUMINIUMOXID ALS TRAEGERMATERIAL FUER EINEN ALUMINIUMOXID- TRAEGERKATALYSATOR

PYROGENES SILICON DIOXIDE POWDER AND DISPERSION OF IT

PROCEDURE FOR THE CONTINUOUS PRODUCTION OF A PERFLUORALKYLIODID TELOMERS

VERFAHREN ZUR SELEKTIVEN HYDRIERUNG VON C2- -MINUS-FRAKTIONEN

VERFAHREN ZUR KONTINUIERLICHEN HERSTELLUNG VON NIEDEREN ALKOHOLEN, INSBESONDERE ISOPROPANOL

PROCEDURE FOR THE CONTINUOUS PRODUCTION OF LOW ALCOHOLS, IN PARTICULAR ISOPROPANOL

PROCEDURE FOR THE CONTINUOUS PRODUCTION OF LOW ALCOHOLS, IN PARTICULAR ISOPROPANOL

CATALYSTS WITH COVERAGE OF THE CARRIERS WITH INCREASED MACRO PRIORITY.

HYDROGENATION CATALYST OF POLYMERS.

HYDROGENIERUNGSKATALYSATOR.

CONTINUOUS PRODUCTION OF LOWER ALCOHOLS

HIGH TEMPERATURE STABLE CATALYST

Reactor and process for Fischer-Tropsch synthesis

PREPARATION OF SUPPORTE NICKEL CATALYST

CATALYST CARRIERS

Cobalt catalysts

ATTRITION RESISTANT METAL OXIDE CATALYST COMPOSITION

ALKYLENE OXIDES AND CATALYSTS THEREFOR

ZIRCONIA CONTAINING SUPPORT MATERIAL FOR CATALYSTS

The present invention addresses at aeast four different aspects relating to catalyat structure, method of making those catalysts and methods of using those catalysts for making allcenyl alkanoates. Separately or together in combination, the various aspects of the invention are directed at improving the production of alkenyl alkanoates and VA in particular, including reduction of by-products and improved production efficiency. A first aspect of the presente invention pertains to a unique palladium/gold catalyst or pre- catalyst (optionally calcined) that includes rhodium or another metal. A second aspect pertains to a palladium/gold catalyst or precatalyst at is based on a layered support material where one layer of the support materiel is substantially free of catalytic components. A third aspect pertains to a palladium/gold catalyst or precatalysts on a zirconia containing support material. A fourth aspect pertains to a palladium gold catalyst or pre- catalyst that is produced from substantially ...

COMPOSITIONS AND METHODS FOR HIGH TEMPERATURE STABLE CATALYSTS

CERAMIC CATALYST CARRIERS FOR THE EXPOXIDATION OF OLEFINS

The selectivity and activity of a silver-based olefin epoxidation catalyst is found to be a function of the pore size distribution in the alumina carrier on which it is deposited. Specifically it is found advantageous to provide a carrier which has a minimum of very large pores, ( greater than 10 micrometers) and a water absorption of 35 to 55% and a surface area of at least 1.0 m2 /g. A method of making such carriers is also described.

PROCESS FOR THE EPOXIDATION OF AN OLEFIN USING A SUPPORTED CATALYST

The invention is a process for the epoxidation of an olefin, wherein the concentration of the olefin oxide in the outlet is greater than about 2.2 vol % with the use of an epoxidation catalyst. The catalyst which has improved selectivity in the epoxidation process, includes a bimodal support, with a first mode of pores that have a diameter ranging from about 0.01 to about microns and having a differential pore volume peak in the range from about 0.01 to about 5 microns and a second mode of pores, which is different from the first mode of pores, having a diameter ranging from about 1 to about 20 microns and have a differential pore volume peak in the range from about 1 to 20 microns. On the surface is a catalytically effective amount of silver, a promoting amount of rhenium, and a promoting amount of one or more alkali metals.

A SILVER-CATALYST COMPOSITION, A PROCESS FOR PREPARING THE CATALYST COMPOSITION AND A USE OF THE CATALYST COMPOSITION FOR THE EPOXIDATION OF ETHYLENE

... ²²²A catalyst composition comprising a support having a surface area of at least ²500 m2/kg, and deposited on the support: - silver metal, - a metal or ²component comprising rhenium, tungsten, molybdenum or a nitrate- or nitrite-²forming compound, and - a Group IA metal or component comprising a Group IA ²metal having an atomic number of at least 37, and in addition potassium, ²wherein the value of the expression (Qk / R) + QHIA is in the range of from ²1.5 to 30 mmole/kg, wherein QHIA and QK represent the quantities in mmole/kg ²of the Group IA metal having an atomic number of at least 37 and potassium, ²respectively, present in the catalyst composition, the ratio of QHIA to QK is ²at least 1:1, the value of QK is at least 0.01 mmole/kg, and R is a ²dimensionaless number in the range of from 1.5 to 5, the units mmole/kg being ²relative to the weight of the catalyst composition.² ...

SILVER BASED CATALYSTS FOR THE PRODUCTION OF OLEFIN OXIDES

Catalyseurs à base d'argent pour la synthèse en phase vapeur des époxydes par réaction d'oxygène, ou de mélange gazeux en contenant, sur un hydrocarbure éthylènique. Les catalyseurs de l'invention sont caractérisés en ce qu'ils renferment à titre de support des graphites artificiels poreux ou des matériaux graphités poreux, présentant une surface spécifique inférieure à 10 m2/g, une granulomètrie de 50 microns à 10 mm et un volume total de porosité compris entre 0.1 et 0,4 cm3/g. Ces catalyseurs sont particulièrement utiles dans la préparation de l'oxyde d'éthylène par époxydation.

ATTRITION RESISTANT METAL/OXYGEN COMPOSITIONS

Attrition resistant metal/oxygen compositions comprising the infusion and rection product of a refractory material characterized by a melting point of at least 1500.degree.C, a mean particle size from about 10.mu.m to about 200.mu.m, and a fractional porosity of at least 0.2, and at least one metal oxide, or compound convertible by heat to such metal oxide, having a maximum mean particle size of about 100.mu.m, with the proviso that the refractory material/metal oxide mean particle size ratio is at least 2, which metal oxide is suscetible of undergoing infusion and reaction with the refractory material upon being subjected to temperatures of at least 0.4Tm for a time sufficient to cause infusion and reaction between the metal oxide and the refractory material, wherein Tm is the melting point in .degree.K of the refractory material, are useful in a wide variety of metal oxidecatalyzed reactions. The compositions are especially useful in reaction which involve reaction conditions of high ...

PROCESS FOR PREPARING AN OXIDATION CATALYST COMPOSITION

A process for preparing an oxidation catalyst composition comprises mixing at least one crystalline composite oxide, as the first component, selected from the group consisting of (i) a crystalline composite oxide containing vanadium and phosphorus and showing the characteristic X-ray diffraction peaks as identified in the following Table A and (ii) a crystalline composite oxide containing vanadium and phosphorus and showing the characteristic X-ray diffraction peaks as identified in the following Table B, an aqueous solution , as the second component, containing vanadium and phosphorus, and silica sol, as the third component, to form an aqueous slurry, spray-drying the slurry, and calcining the solid particles thereby obtained: < IMG > ...

CATALYSTS WITH SUPPORT COATINGS HAVING INCREASED MACROPOROSITY

CATALYSTS WITH SUPPORT COATINGS HAVING INCREASED MACROPOROSITY A catalyst composition comprises a carrier having a refractory metal oxide support coating thereon and a catalytic platinum group metal dispersed on the support coating. A major portion of the support coating is comprised of a conventional, first metal oxide such as stabilized gamma alumina and a minor portion is provided by a macroporous, second metal oxide such as cordierite. The second metal oxide is conveniently provided by comminuting finished catalyst production scrap. In the method of the invention particles of the first metal oxide are combined with particles of the second metal oxide to form the coating.

CATALYSTS SPUTTERED ON LOW SURFACE AREA PARTICULATE SUPPORTS

In catalytic gas phase reactions there is used catalyst comprising a sputtered deposit of catalytic material equivalent to between 0.5 and 5 monatomic layers upon a hard, substantially non-porous substrate. The substrate being hard and non-porous is of low surface area, that is not greater than 20 square metres per gram, and preferably cmmprises particles having a size in the range 0.1 micron to 0.5 centimetres.

PROCESS FOR THE MANUFACTURE OF A COBALT MOLYBDATE CATALYST

PROCESS FOR PREPARING A HIGH-DENSITY AND MIDDLE-POROSITY CATALYST, SUPPORTED ON A SILICEOUS MATRIX, BASED ON VANADIUM

A process for preparing a high-density and middle-po-rosity catalyst, supported on a siliceous matrix, based on vanadium, oxygen and alkali metals, wherein the V2O5 content ranges from 6 to 9% by weight, the K2O content ranges from 8.5 to 12% by weight and the particle density ranges from 0.90 to 1.40 g/cm3 and wherein furthermore: - the volume of the pores is from 0.30 to 0.70 cm3/g and the surface area is from 0.30 to 3 m2/g, the average radius of the pores being from 650 to 2200 nanometers; - the SiO2 content is equal to or lower than 75% by weight and the Fe2O3 content is equal to or higher than 0.90% by weight.

PROCESS FOR THE CONTINUOUS PRODUCTION OF LOWER ALIPHATIC ALCOHOLS

CARBON AND EROSION RESISTANT CATALYST

OXIDATION CATALYST AND ITS PREPARATION

The present invention provides a method of preparation of a supported catalyst composition suitable for the oxidation of ethane to ethylene and/or acetic acid, and/or the oxidation of ethylene to acetic acid, which supported catalyst composition comprises a catalyst, comprising one or more metal components, on a support comprising alpha-~alumina, and which method comprises (a) forming a slurry comprising the one or more metal components, and alpha- alumina support particles or an alpha-alumina support precursor, (b) spray- drying the slurry, and, optionally, (c) calcining the spray-dried slurry to form the supported catalyst composition. The present invention also provides a supported catalyst composition formed by the above method, and a process for the selective oxidation of ethane to ethylene and/or acetic acid, and/or the selective oxidation of ethylene to acetic acid utilising the supported catalyst composition.

LOW SURFACE AREA ALUMINA

A CATALYST, A PROCESS FOR PREPARING THE CATALYST, AND A PROCESS FOR THE PRODUCTION OF AN OLEFIN OXIDE, A 1,2-DIOL, A 1,2-DIOL ETHER, OR AN ALKANOLAMINE

A catalyst which comprises a carrier and silver deposited on the carrier, which carrier has a surface area of at least 1.3 m2/g, a median pore diameter of more than 0.8 ~m, and a pore size distribution wherein at least 80 % of the total pore volume is contained in pores with diameters in the range of from 0.1 to 10 ~m and at least 80 % of the pore volume contained in the pores with diameters in the range of from 0.1 to 10 ~m is contained in pores with diameters in the range of from 0.3 to 10 ~m; process for the preparation of a catalyst which process comprises depositing silver on a carrier, wherein the carrier has been obtained by a method which comprises forming a mixture comprising: a) from 50 to 95 weight percent of a first particulate a-alumina having a median particle size (d50) of from 5 to 100 ~m; b) from 5 to 50 weight percent of a second particulate a-alumina having a d50 which is less than the d50 of the first particulate a-alumina and which is in the range of from 1 to 10 ~m ...

A CATALYST CARRIER AND A PROCESS FOR PREPARING THE CATALYST CARRIER

A carrier, which comprises non-platelet alumina and/or a bond material, has a surface area of at least 1 m2/g, a total pore volume and a pore size distribution such that at least 80 % of the total pore volume is contained in pores with diameters in the range of from 0.1 to 10 .mu.m, and at least 80 % of the pore volume contained in the pores with diameters in the range of from 0.1 to 10 .mu.m is contained in pores with diameters in the range of from 0.3 to 10 .mu.m, and a process for the preparation of a carrier which comprises forming a mixture comprising: a) from 50 to 95 weight percent of a first particulate .alpha.- alumina having a median particle size (d50) of from 5 to 100 .mu.m; b) from 5 to 50 weight percent of a second particulate .alpha.- alumina having a d50 which is less than the dso of the first particulate .alpha.-alumina and which is in the range of from 1 to 10 .mu.m; and c) an alkaline earth metal silicate bond material; weight percent being based on the total weight of ...

SILVER BASED CATALYSTS FOR THE PRODUCTION OF OLEFIN OXIDES

DEHYDROGENATION CATALYST

Provided is a dehydrogenation catalyst with which it is possible to suppress caulking and increase the yield of an olefin in a thermal decomposition reaction of a hydrocarbon raw material. This dehydrogenation catalyst (4A) used in the manufacture of an olefin contains at least one element of La and Ce as a catalyst component. The dehydrogenation catalyst (4A) contains at least one element selected from the group consisting of Ba, Fe, and Mn when the dehydrogenation catalyst (4A) does not contain Ce. The dehydrogenation catalyst (4A) contains at least one element of Fe and Mn when the dehydrogenation catalyst (4A) contains Ce.

CATALYST EFFECTIVE IN THE OXIDATIVE CONVERSION OF ETHYLENE TO ETHYLENE OXIDE

The present invention provides a catalyst effective in the oxidative conversion of ethylene to ethylene oxide, comprising an alumina support and 20 to 45 % by weight of the catalyst, of silver applied to the support, the catalyst meeting the following limitations (i) to (v): (i) an amount of cesium c(Cs) in mmol per Kg of catalyst of at least 2; (ii) an amount of rhenium c(Re) in mmol per Kg of catalyst of at least 3.0; (iii) an amount of tungsten c(W) in mmol per Kg of catalyst of at least 1.6; (iv) a silicon to alkaline earth metal molar ratio x of not higher than 1.80; (v) c(Cs) c(Re) c(W) = 4 · x 0.5.

BASE METAL DEWAXING CATALYST

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

SELECTIVE HYDROGENATION METHODS AND CATALYSTS

The present disclosure relates to methods for selectively hydrogenating acetylene, to methods for starting up a selective hydrogenation reactor, and to hydrogenation catalysts useful in such methods. In one aspect, the disclosure provides a method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition with a process gas. The catalyst composition comprises a porous support, palladium, and one or more ionic liquids. The process gas includes ethylene, present in the process gas in an amount of at least 20 mol.%; and acetylene, present in the process gas in an amount of at least 1 ppm. At least 90% of the acetylene present in the process gas is hydrogenated, and the selective hydrogenation is conducted without thermal runaway. Notably, the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) based on total catalyst volume in one bed or multiple beds of at least 7,100 h-1.

NOBLE METAL AND BASE METAL DEWAXING CATALYST

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

LONG CHAIN BRANCHED POLYMERS AND METHODS OF MAKING SAME

A polymer having a long chain branching content peaking at greater than about 20 long chain branches per million carbon atoms, and a polydispersity index of greater than about wherein the long chain branching decreases to approximately zero at the higher molecular weight portion of the molecular weight distribution. A polymer having a long chain branching content peaking at greater than about 8 long chain branches per million carbon atoms, a polydispersity index of greater than about 20 wherein the long chain branching decreases to approximately zero at the higher molecular weight portion of the molecular weight distribution. A polymer having a long chain branching content peaking at greater than about 1 long chain branches per chain, and a polydispersity index of greater than about 10 wherein the long chain branching decreases to approximately zero at the higher molecular weight portion of the molecular weight distribution.

CATALYST AND PROCESS FOR IMPROVING THE ADIABATIC STEAM-REFORMING OF NATURAL GAS

A process for adiabatically prereforming a feedstock, includes: providing an adiabatic reactor; providing a catalyst containing 1-20 wt.% nickel and 0.4-5 wt.% potassium, wherein the catalyst has an overall catalyst porosity of 25-50% with 20-80% of the overall catalyst porosity contributed by pores having pore diameters of at least 500.ANG.; providing the feedstock containing natural gas and steam, wherein the natural gas contains an initial concentration of higher hydrocarbons, and a ratio of steam to natural gas in the feedstock is from 1.5:1 to 5:1; preheating the feedstock to a temperature of 300-700.degree.C to provide a heated feedstock; providing the heated feedstock to the reactor; and producing a product containing hydrogen, carbon monoxide, carbon dioxide, unreacted methane, and steam, wherein said product contains a reduced concentration of higher hydrocarbons less than the initial concentration of higher hydrocarbons, to prereform the feedstock.

HYDROTHERMAL PRETREATMENT FOR INCREASING AVERAGE PORE SIZE IN CATALYST SUPPORTS

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

ZIRCONIA CONTAINING SUPPORT MATERIAL FOR CATALYSTS

The present invention addresses at aeast four different aspects relating to catalyat structure, method of making those catalysts and methods of using those catalysts for making allcenyl alkanoates. Separately or together in combination, the various aspects of the invention are directed at improving the production of alkenyl alkanoates and VA in particular, including reduction of by-products and improved production efficiency. A first aspect of the presente invention pertains to a unique palladium/gold catalyst or pre- catalyst (optionally calcined) that includes rhodium or another metal. A second aspect pertains to a palladium/gold catalyst or precatalyst at is based on a layered support material where one layer of the support materiel is substantially free of catalytic components. A third aspect pertains to a palladium/gold catalyst or precatalysts on a zirconia containing support material. A fourth aspect pertains to a palladium gold catalyst or pre- catalyst that is produced from substantially ...

EXHAUST GAS PURIFICATING CATALYST

An exhaust gas purification catalyst that breaking the warring relationsh ip between Hg oxidation and SO2 oxidation as a limit of conventional catalys ts, realizes lowering only the SO2 oxidation ratio while maintaining the Hg oxidation ratio at a high level. There is provided an exhaust gas purificati on catalyst consisting of a composition comprising respective oxides of (i) titanium (Ti), (ii) molybdenum (Mo) and/or tungsten (W), (iii) vanadium (V) and (iv) phosphorus (P) wherein the atomic ratio of Ti : (Mo and/or W) : V i s 85 to 97.5 : 2 to 10 : 0.5 to 10, and wherein the atomic ratio of P/(sum o f Mo and/or W and V) is inthe range of 0.5 to 1.5. Further, there is provide d a method of exhaust gas purification characterized in that an exhaust gas containing nitrogen oxide (NOx) and metallic mercury (Hg) is brought into co ntact with the above catalyst in the presence of ammonia as a reducing agent so as to carry out oxidation of metallic mercury (Hg) and reduction of NOx contained ...

HYDROMETALLURGICAL PROCESS FOR PRODUCTION OF SUPPORTED CATALYSTS

... ²²²A process for the production of a supported catalyst. The process comprises ²heating a slurry that comprises a catalyst support and at least one active ²catalytic ingredient precursor. Gas is introduced to the slurry at a ²sufficient pressure to reduce the at least one active catalytic ingredient ²precursor and deposit at least one active catalytic ingredient onto a surface ²of the catalyst support to form the supported catalyst. The supported catalyst ²has a large active catalytic surface area.² ...

STABILIZATION OF BULK CATALYSTS WITH ORGANO-METALLOXANE FRAMEWORK

Bulk metallic catalyst precursor compositions are provided that include a Group VIB metal, a Group VIII metal, an organic-compound based component, and an organo-metalloxane polymer or gel. The catalyst precursor compositions can further include a binder. Amorphous sulfided catalysts formed from the catalyst precursor compositions are also provided. The catalyst precursor compositions can have a surface area of about 20 m2/g or less.

RETAINING MATERIAL FOR POLLUTION CONTROL ELEMENT, METHOD FOR MANUFACTURING THE SAME, AND POLLUTION CONTROL DEVICE

A retaining material that can sufficiently maintain the function of retaining a pollution control element in a pollution control device at high temperature. In one aspect, the retaining material has a mat shape and contains inorganic fiber material, with the retaining material containing: a surface layer containing inorganic colloid particles; and an internal region positioned further to the inside than the surface layer, impregnated with inorganic colloid particles and organic binder; wherein the surface layer contains inorganic colloid particles at a higher concentration than the internal region; and the amount of inorganic colloid particles in the internal region is 1 mass% to 10 mass% based on the total mass of the retaining material.

AGGLOMERATED ODH CATALYST

Oxidative dehydrogenation catalysts for converting lower paraffins to alkenes such as ethane to ethylene when prepared as an agglomeration, preferably extruded with supports consisting of slurries of Nb2O5.

SILVER CATALYSTS WITH IMPROVED SIZE AND DISTRIBUTION DENSITY OF SILVER PARTICLES

A silver-based ethylene epoxidation catalyst is provided that exhibits improved performance, i.e., selectivity and activity decline. The catalyst that exhibits the improved performance includes greater than about 20 % by weight of silver disposed on an alpha-alumina carrier, and a promoting amount of one or more promoters disposed on the alpha-alumina carrier. The silver is present on the alpha-alumina carrier as silver particles having a diameter of greater than about 150 nm and a distribution density of about 20 particles per 1 square micron or less.

TITANIUM DIOXIDE BASED PHOTOCATALYTIC COMPOSITES AND DERIVED PRODUCTS ON A METAKAOLIN SUPPORT

Described herein is a photocatalytic composite comprising a titanium dioxide supported on metakaolin. In comparison to known embodiments of the sector, the composite of the present invention makes it possible to obtain binders and derived products with high photocatalytic efficiency, even when using photocatalyst quantities which are lesser than those present in products of prior technical art.

AMMONIA SYNTHESIS CATALYST AND AMMONIA SYNTHESIS METHOD

The present invention provides a catalyst substance that is stable and performs well in the synthesis of ammonia, one of the most important chemical substances for fertilizer ingredients and the like. The catalyst substance exhibits catalytic activity under mild synthesis conditions not requiring high pressure, and is also advantageous from a resource perspective. Further provided is a method for producing the same. This catalyst comprises a supported metal catalyst having a mayenite compound, containing a conduction electron of 1015cm-3 or more, as a carrier for the ammonia synthesis catalyst. The mayenite compound used as the carrier may take any shape, including that of powder, a porous medium, a solid sintered body, a thin-film, or a solid single crystal. Use of this catalyst makes it possible for the electron donor ability toward a transition metal to be large, and to promote ammonia synthesis by reacting the starting material nitrogen and hydrogen on the catalyst under low reactive ...

A PROCESS FOR THE PRODUCTION OF ETHYLENICALLY UNSATURATED CARBOXYLIC ACIDS OR ESTERS AND A CATALYST THEREFOR

A method of producing an ethylenically unsaturated carboxylic acid or ester such as (meth) acrylic acid or alkyl esters thereof, for example, methyl methacrylate is described. The process comprises the steps of contacting formaldehyde or a suitable source thereof with a carboxylic acid or ester, for example, propionic acid or alkyl esters thereof in the presence of a catalyst and optionally an alcohol. The catalyst comprises group II metal phosphate crystals having rod or needle like morphology or a suitable source thereof. The phosphate may be a hydroxyapatite, pyrophosphate, hydroxyphosphate, PO4 2-phosphate or mixtures thereof. The group II metal may be selected from Ca, Sr, Ba or mixtures thereof, for example, strontium hydroxyapatite and calcium hydroxyapatite. A catalyst system comprising a crystalline metal phosphate catalyst and a catalyst support is also described. The metal phosphate has rod/needle like morphology.

Rh-C3N4 HETEROGENEOUS CATALYST FOR PREPARING ACETIC ACID BY CARBONYLATION REACTION

This invention relates to a catalyst for use in the preparation of acetic acid through a methanol carbonylation reaction using carbon monoxide, and particularly to a heterogeneous catalyst represented by Rh/C 3 N 4 configured such that a complex of a rhodium compound and 3-benzoylpyridine is immobilized on a carbon nitride support.

A CATALYST COMPOSITION AND ITS APPLICATIONS THEREOF

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

CATALYST COMPOSITIONS AND PROCESS FOR DIRECT PRODUCTION OF HYDROGEN CYANIDE IN AN ACRYLONITRILE REACTOR FEED STREAM

The present invention relates to catalyst compositions containing a mixed oxide catalyst of formula (I) or formula (II) as described herein, their preparation, and their use in a process for ammoxidation of various organic compounds to their corresponding nitriles and to the selective catalytic oxidation of excess NHpresent in effluent gas streams to Nand/or NO. 1. A catalyst composition comprising a mixed oxide catalyst of formula (I) or (II):{'br': None, 'sub': 12', 'a', 'b', 'c', 'd', 'e', 'f', 'h, 'sup': 1', '2', '3', '4', '5', '6, 'MoXXXXXXO\u2003\u2003(I)'}{'br': None, 'sub': i', 'j', 'k', 'm', 'n', 'q', 'x', 'y', 'r, 'FeMoCrBiMNQXYO\u2003\u2003(II)'} [{'sup': '1', 'Xis Cr and/or W;'}, {'sup': '2', 'Xis Bi, Sb, As, P, and/or a rare earth metal;'}, {'sup': '3', 'Xis Fe, Ru, and/or Os;'}, {'sup': '4', 'Xis Ti, Zr, Hf, B, Al, Ga, In, TI, Si, Ge, Sn, and/or Pb;'}, {'sup': '5', 'Xis Co, Rh, Ir, Ni, Pd, Pt, Cu, Ag, Au, Zn, Cd, Hg, Mn, Re, V, Nb, Ta, Se, and/or Te;'}, {'sup': '6', 'Xis an alkaline earth metal and/or an alkali metal;'}, '0≤a≤5;', '0.03≤b≤25;', '0≤c≤20;', '0≤d≤200;', '0≤e≤8;', '0≤f≤3; and', 'h is the number of oxygen atoms required to satisfy the valence requirements of the component elements other than oxygen present in formula (I), where', '1≤c+d+e+f≤200;', '0≤e+f≤8; and, 'wherein in the formula (I) M is Ce and/or Sb;', 'N is La, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, Ti, Zr, Hf, B, Al, Ga, In, TI, Si, Ge, Sn, Pb, P, and/or As;', 'Q is W, Ru, and/or Os;', 'X is Co, Rh, Ir, Ni, Pd, Pt, Cu, Ag, Au, Zn, Cd, Hg, Mn, Re, V, Nb, Ta, Se, and/or Te;', 'Y is an alkaline earth metal and/or an alkali metal;', '0.2≤i≤100;', '0≤j≤2;', '0≤k≤2;', '0.05≤m≤10;', '0≤n≤200;', '0≤q≤8;', '0≤x≤30;', '0≤y≤8;', 'j and kj; and', 'r is the number of oxygen atoms required to satisfy the valence requirements of the component elements other than oxygen present in formula (II),, 'wherein in the formula (II) 4≤m+n+q+x+y≤200;', '0≤q+x+y≤30; and, 'wherein{'sup ...

CATALYST FOR THE CONVERSION OF NATURAL OR ASSOCIATED GAS INTO SYNTHESIS GAS IN AN AUTOTHERMAL REFORMING PROCESS AND METHOD FOR PREPARING THE SAME

A catalyst in a calcined state has a specific surface area of 20-50 m/g of catalyst, and a specific surface area of nickel metal after reduction of the catalyst of 8 to 11 m/g, wherein the average particle size of nickel metal is 3-8 nm, the dispersion of the particles is 10-16%, and the content of nickel is 5-15 wt. % based on the weight of calcined catalyst. A support has a specific surface area of 40-120 m/g with a pore volume of the support of 0.2-0.4 cm/g, wherein the support is selected from a mixture of zirconium oxide and cerium oxide or magnesium oxide, cerium oxide and the ballast being zirconium oxide. The catalyst further contains a promoter selected from the group consisting of palladium and ruthenium, in an amount of from 0.01 to 0.5 wt. %. The catalyst is prepared by co-precipitation with ammonium hydroxide from a solution containing nickel, cerium and zirconium precursors and distilled water or from a solution containing nickel, cerium, zirconium, and magnesium precursors and distilled water, and having a pH of 8.0-9.0. The process is carried out under agitation at a temperature of 40-45° C. for 1-2 hours, followed by filtration, drying at a temperature of 100-110° C. for 6-8 hours, and calcining at a temperature of 400-650° C. for 4-6 hours. The invention provides a high average conversion of natural/associated gas of at least 90% in an autothermal reforming reaction of natural or associated gas, and a high synthesis gas output of at least 7000 m/m·h. 1. A catalyst for the conversion of natural/associated gas to synthesis-gas in an autothermal reforming process , having a specific surface area in a calcined state of 20 to 50 m/g of catalyst and a specific surface area of nickel metal after reduction of the catalyst of 8 to 11 m/g , an average nickel metal particles of 3 to 8 nm , and a particle dispersion of 10 to 16% , the catalyst comprising from 5 to 15 wt. % of nickel based on the weight of the calcined catalyst , and a support having a specific ...

METHOD FOR MANUFACTURING AMMONIA SYNTHESIS CATALYST, AND METHOD FOR MANUFACTURING AMMONIA

Provided is a method for manufacturing a catalyst with which it is possible to obtain a supported metal ammonia synthesis catalyst, in which there are restrictions in terms of producing method and producing facility, and particularly large restrictions for industrial-scale producing, in a more simple manner and so that the obtained catalyst has a high activity. This method for manufacturing an ammonia synthesis catalyst includes: a first step for preparing 12CaO.7AlOhaving a specific surface area of 5 m/g or above; a second step for supporting a ruthenium compound on the 12CaO.7AlO; and a third step for performing a reduction process on the 12CaO.7AlOsupporting the ruthenium compound, obtained in the second step. This invention is characterized in that the reduction process is performed until the average particle diameter of the ruthenium after the reduction process has increased by at least 15% in relation to the average particle diameter of the ruthenium before the reduction process. 1. A method for manufacturing ammonia , comprising:{'sub': 2', '3, 'sup': '2', 'a first step of preparing 12CaO.7AlOhaving a specific surface area of 5 m/g or more;'}{'sub': 2', '3, 'a second step of supporting a ruthenium compound on the 12CaO.7AlO;'}{'sub': 2', '3, 'a third step of performing reduction process on the 12CaO.7AlOon which a ruthenium compound is supported (hereinafter referred to as ruthenium-supported C12A7) obtained in the second step, wherein the reduction process is carried out until an average particle diameter of a ruthenium after the reduction process increases by 15% or more with respect to an average particle diameter of a ruthenium before the reduction process; and'}a step of producing ammonia by contacting a gas containing nitrogen and hydrogen with an ammonia synthesis catalyst which is obtained by the reduction process in the third step.2. The method according to claim 1 , wherein in the step of performing reduction process claim 1 , the reduction process ...

CATALYSTS AND METHODS FOR NATURAL GAS PROCESSES

Catalysts and catalytic methods are provided. The catalysts and methods are useful in a variety of catalytic reactions, for example, the oxidative coupling of methane. 1. A catalyst comprising the following formula (IA):{'br': None, 'sub': x', 'y', 'v', 'w', 'z, 'ABCDO\u2003\u2003 (IA)'}wherein:A is a lanthanide or group 4 element;B is a group 2 element;C is a group 13 element;D is a lanthanide element;O is oxygen;v and w are independently numbers greater than 0;{'sub': x', 'y', 'v', 'w', 'z, 'x, y and z are independently numbers greater than 0, and v, w, x, y and z are selected such that ABCDOhas an overall charge of 0.'}2. The catalyst of claim 1 , wherein A is a lanthanide.3. The catalyst of claim 2 , wherein A is lanthanum claim 2 , cerium claim 2 , praseodymium or neodymium.4. The catalyst of claim 1 , wherein A is a Group 4 element.5. The catalyst of claim 4 , wherein A is titanium claim 4 , zirconium or hafnium.6. The catalyst of claim 1 , wherein B is magnesium claim 1 , calcium claim 1 , strontium or barium.7. The catalyst of claim 1 , wherein A is lanthanum and B is strontium claim 1 , A is cerium and B is barium claim 1 , A is praseodymium and B is barium claim 1 , A is cerium and B is strontium claim 1 , A is titanium and B is barium claim 1 , A is titanium and B is strontium or A is titanium and B is calcium.8. The catalyst of claim 1 , wherein C is aluminum claim 1 , gallium claim 1 , indium or thallium.9. The catalyst of claim 1 , wherein D is lanthanum claim 1 , neodymium claim 1 , gadolinium or ytterbium.10. The catalyst of claim 1 , wherein:A is titanium, zirconium or cerium;B is calcium, strontium or barium;C is aluminum, gallium or indium; andD is lanthanum, neodymium; gadolinium or ytterbium.11. The catalyst of claim 1 , comprising one of the following formulas: CeBaInNdO; TiCaInLaO; TiCaInNdO; TiCaInGdO; TiCaInYbO; ZrCaInLaO; ZrCaInNdO; ZrCaInGdO; ZrCaInYbO; CeCaInLaO; ZrCaInNdO; ZrCaInGdO; ZrCaInYbO; TiSrInLaO; TiSrInNdO; TiSrInGdO; TiSrInYbO; ...

Diethyl Oxalate Catalysts

A highly effective catalyst for the preparation of diethyl oxalate using carbon monoxide using Pd/α-AlOand CeOas a promoter. High conversion rates with greatly extended catalyst life is achieved with the CeO-enhanced Pd catalysts. The catalysts can be used for the production of high-value diethyl oxalate, and eventually ethylene glycol, from coal-derived syngas. 1. A highly effective catalyst for the preparation of diethyl oxalate using carbon monoxide , comprising Pd/α-Al2O3 and CeOas a promoter.2. A catalyst of claim 1 , wherein the loading of Pd is between 0.1 wt % and 3 wt %.3. A catalyst of claim 2 , wherein the loading of Pd is between 0.6 wt % and 1.2 wt %.4. A catalyst of claim 1 , wherein the loading of CeOis between 0.02 wt % and 1.0 wt %.5. A catalyst of claim 4 , wherein the loading of CeOis between 0.15 wt % and 0.25 wt %.6. A catalyst of claim 1 , wherein the Pd is present in the form of particles and the average size of the Pd particles is between 2 nm and 80 nm and the average surface area of the Pd particles is between 1 and 20 m/g.7. A catalyst of wherein the carbon monoxide is from coal-derived syngas.8. A method of improving the conversion rate of carbon monoxide to diethyl oxalate by catalysts comprising Pd/α-AlO claim 1 , comprising using CeOas an enhancer.9. A method of improving the conversion rate of carbon monoxide to diethyl oxalate by catalysts comprising Pd/α-AlOand extending the time the catalyst conversion rate remains high claim 1 , comprising using CeOas an enhancer. This application claims priority to U.S. patent application Ser. No. 62/018,471, filed Jun. 27, 2014, and which is incorporated herein in its entirety by this reference.The present invention relates generally to catalysts of the production of diethyl oxalate from carbon dioxide and, more specifically, to highly effective palladium catalysts promoted with cerium.Ethylene glycol (EG) is a crucial raw material with a global demand of around 25 million tons each year, which ...

Improved Catalyzed Soot Filter

A catalyzed soot filter, in particular for the treatment of Diesel engine exhaust, comprises a coating design which ensures soot particulates filtration, assists the oxidation of carbon monoxide (CO), and produces low HS emissions during normal engine operations and regeneration events. 1. A catalyzed soot filter , comprisinga wall flow substrate comprising an inlet end, an outlet end, a substrate axial length extending between the inlet end and the outlet end, and a plurality of passages defined by internal walls of the wall flow filter substrate;wherein the plurality of passages comprise inlet passages having an open inlet end and a closed outlet end, and outlet passages having a closed inlet end and an open outlet end;wherein the internal walls of the inlet passages comprise an inlet coating comprising at least one layer, and the inlet coating extends from the inlet end to an inlet coating end, thereby defining an inlet coating length, wherein the inlet coating length is x % of the substrate axial length, with 25≦x≦100; andwherein the internal walls of the outlet passages comprise an outlet coating comprising at least one layer, and the outlet coating extends from the outlet end to an outlet coating end, thereby defining an outlet coating length, wherein the outlet coating length is y % of the substrate axial length, with 25≦y≦100;wherein the inlet coating length defines an upstream zone of the catalyzed soot filter and the outlet coating length defines a downstream zone of the catalyzed soot filter;{'sub': '2', 'wherein the wall flow substrate comprises at least one layer comprising at least one oxidation catalyst and at least one layer comprising at least one HS suppressing material;'}{'sub': '2', 'wherein said at least one oxidation catalyst and said at least one HS suppressing material are separated by the internal walls of the wall flow filter substrate;'}characterized in that the total coating length is x+y, and x+y≧100.2. The catalyzed soot filter of claim ...

POROUS BODIES WITH ENHANCED PORE ARCHITECTURE

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

OZONE-ACTIVATED NANOPOROUS GOLD AND METHODS OF ITS USE

The invention relates to nanoporous gold nanoparticle catalysts formed by exposure of nanoporous gold to ozone at elevated temperatures, as well as methods for production of esters and other compounds. 1. A method of synthesizing an activated nanoporous gold catalyst , the method comprising the steps of:a. providing nanoporous gold comprising 0.1 to 10% silver by atom; andb. contacting the nanoporous gold with ozone at a temperature of 100° C. or greater for a time sufficient to form the activated nanoporous gold catalyst.2. The method of claim 1 , wherein the nanoporous gold is formed by diminishing the quantity of silver present within an alloy comprising gold and silver.3. The method of claim 2 , wherein the alloy comprises from 70 to 85% silver by atom.4. The method of or claim 2 , wherein the diminishing comprises mixing the alloy with a solution comprising nitric acid.5. The method of any one of - claim 2 , wherein the nanoporous gold catalyst comprises from 1 to 3% silver by atom.6. The method of any one of - claim 2 , wherein the ozone is present within a mixture comprising one or more gases at a concentration of from 10 to 50 g/Nm.7. The method of claim 6 , wherein the one or more gases are selected from the group consisting of Oand He.8. The method of any one of - claim 6 , wherein the contacting comprises flowing the ozone at a rate of from 30 to 70 mL/min.9. The method of any one of - claim 6 , wherein the nanoporous gold catalyst is a foil.10. The method of claim 9 , wherein the foil has a pore depth of from 25 to 75 nm.11. The method of any one of - claim 9 , wherein the foil is characterized by a ligament width of from 15 to 45 nm.12. The method of any one of - claim 9 , wherein the nanoporous gold catalyst is an ingot.13. The method of claim 12 , wherein the ingot is characterized by a ligament width of from 25 to 75 nm.14. The method of any one of - claim 12 , wherein the ingot has a surface area of from 2 to 6 m/g.15. The method of any one of - ...

CATALYTIC FORMS AND FORMULATIONS

Catalytic forms and formulations are provided. The catalytic forms and formulations are useful in a variety of catalytic reactions, for example, the oxidative coupling of methane. Related methods for use and manufacture of the same are also disclosed. 152-. (canceled)53. A catalytic material comprising a first and second catalyst , wherein the first and second catalysts have a different catalytic activity in the oxidative coupling of methane (OCM) reaction under the same conditions , wherein the catalytic material comprises a C2 selectivity of greater than 50% and a methane conversion of greater than 20% when the catalyst is employed as a heterogeneous catalyst in the oxidative coupling of methane at a temperature of 750° C. or less.54. The catalytic material of claim 53 , wherein the first catalyst is a nanowire catalyst.55. The catalytic material of claim 53 , wherein the second catalyst is a bulk catalyst.56. The catalytic material of claim 53 , wherein each of the first and second catalysts are nanowire catalysts.57. The catalytic material of claim 53 , wherein each of the first and second catalyst are bulk catalysts.58. The catalytic material of claim 53 , wherein the second catalyst has a lower catalytic activity than the first catalyst under the same conditions.59. The catalytic material of claim 58 , wherein the catalytic activity of the second catalyst increases with increasing temperature.6070-. (canceled)71. The catalytic material of claim 53 , wherein the catalytic material comprises a void fraction volume of about 35% to about 70%.72. The catalytic material of claim 71 , wherein the catalytic material comprises a void fraction volume of about 45% to about 65%.73. The catalytic material of claim 53 , wherein the catalytic material comprises catalyst particles having a cross sectional dimension in at least one dimension between about 1 mm and about 20 mm.74. The catalytic material of claim 73 , wherein the cross sectional dimension is between about 2 mm ...

DECOMPOSITION OF CONDENSATION POLYMERS

Particles of a transition metal are used as a catalyst for depolymerisation of condensation polymers in alcohol. In the method of catalysed depolymerisation of a condensation polymer in a solid form into monomers and/or oligomers, transition metal particles; are mixed with the condensation polymer in alcohol to obtain a reaction mixture. This reaction mixture is processed to disperse the condensation polymer into the alcohol and decompose it, wherein the transition metal particles act as a catalyst and the alcohol is a reagent. The catalyst is particularly supplied as a catalyst composition of transition metal particles in an alcoholic liquid. The transition metal particles are typically non-porous and may have an oxide surface. 1. A method of depolymerisation of condensation polymers in alcohol , wherein use is made of particles of a transition metal as a catalyst for said depolymerisation of condensation polymers.2. The method as claimed in claim 1 , wherein use is made of transition metal particles in the range of 0.5-50 μm.3. The method as claimed in claim 1 , wherein the transition metal particles are at least substantially non-porous.4. The method as claimed in claim 1 , wherein the transition metal particles have a surface area of less than 3 m/g.5. The method as claimed in claim 1 , wherein use is made of iron or nickel particles.6. The method as claimed in claim 5 , wherein the iron particles are obtained by thermal decomposition of iron pentacarbonyl claim 5 , and the nickel particles are obtained by thermal decomposition of nickel tetracarbonyl.7. The method as claimed in claim 5 , wherein the iron particles have an iron oxide surface.811.-. (canceled)12. The method as claimed in claim 1 , wherein the condensation polymer is a waste polymer.13. The method as claimed in claim 1 , wherein the condensation polymer is chosen from the group of polyesters claim 1 , polyamides claim 1 , polyimides and polyurethanes.149. The method as claimed in claim claim 1 , ...

CATALYST FOR ALKANE OXIDATIVE UU DEHYDROGENATION AND/OR ALKENE OXIDATION

The invention relates to a process for preparing a shaped catalyst for alkane oxidative dehydrogenation and/or alkene oxidation, which comprises: a) preparing a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium; b) mixing the catalyst obtained in step a), a binder and optionally water, wherein the binder has a surface area greater than 100 m/g and a water loss upon heating at a temperature of 485° C. which is greater than 1 wt. %; c) shaping the mixture obtained in step b) to form a shaped catalyst by means of tableting; and d) subjecting the shaped catalyst obtained in step c) to an elevated temperature. Further, the invention relates to a catalyst obtainable by said process and to a process of alkane oxidative dehydrogenation and/or alkene oxidation wherein said catalyst is used. 1. A process for preparing a shaped catalyst for alkane oxidative dehydrogenation and/or alkene oxidation , the process comprising:a) preparing a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium;b) mixing the catalyst obtained in step a), a binder and optionally water, wherein the binder has a surface area greater than 100 m2/g and a water loss upon heating at a temperature of 485° C. greater than 1 wt. %, wherein said water loss is represented by the difference between the binder weight after heating the binder at a temperature of 110° C. and the binder weight after heating the binder at a temperature of 485° C., relative to the binder weight after heating the binder at a temperature of 110° C.;c) shaping the mixture obtained in step b) to form a shaped catalyst by means of tableting; andd) subjecting the shaped catalyst obtained in step c) to an elevated temperature.2. The process according to claim 2 , wherein the water loss of the binder is at least 2 wt. %.3. The process according to claim 1 , wherein the surface area of the binder is of from 150 to 500 m2/g.4. The process according to claim 1 , ...

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.

METHOD FOR THE PREPARATION OF C3-C12-ALCOHOLS BY CATALYTIC HYDROGENATION OF THE CORRESPONDING ALDEHYDES

The present invention relates to a process for preparing C-Calcohols by catalytically hydrogenating the corresponding aldehydes at a temperature in the range of 50-250° C. and a pressure in the range of 5-150 bar in the presence of a supported activated Raney-type catalyst, characterized in that the support body is a metal foam and the metal is selected from the group consisting of cobalt, nickel and copper and mixtures thereof. 112-. (canceled)13. A process for preparing C-Calcohols by catalytically hydrogenating the corresponding aldehydes at a temperature in the range of 50-250° C. and a pressure in the range of 5-150 bar in the presence of a supported activated Raney-type catalyst , wherein the supported activated Raney-type catalyst comprises a support body that is a metal foam and the metal is selected from the group consisting of: cobalt; nickel; copper; and mixtures thereof.14. The process of claim 13 , wherein a C-Caldehyde is used in the hydrogenation.15. The process of claim 13 , wherein isononanal or butyraldehyde is used as the aldehyde in the hydrogenation.16. The process of claim 13 , wherein the metal is nickel.17. The process of claim 13 , wherein the supported activated Raney-type catalyst contains 85-95% by weight of nickel and 5-15% by weight of aluminium claim 13 , based on the total weight of the catalyst.18. The process of claim 17 , wherein the supported activated Raney-type catalyst additionally contains up to 3% by weight of molybdenum claim 17 , based on the total weight of the catalyst.19. The process of claim 13 , wherein the supported activated Raney-type catalyst has the following properties:{'sup': '2', 'a) a BET surface area of 1-200 m/g, and'}b) macroscopic pores in the range of 100-5000 μm.20. The process of claim 13 , wherein the supported activated Raney-type catalyst is cylindrical claim 13 , annular claim 13 , cuboidal claim 13 , parallelepipedal or cubic.21. The process of claim 20 , wherein the supported activated Raney-type ...

HIGHLY ACTIVE THERMALLY STABLE NANOPOROUS GOLD CATALYST

In one embodiment, a method includes depositing oxide nanoparticles on a nanoporous gold support to form an active structure and functionalizing the deposited oxide nanoparticles. In another embodiment, a system includes a nanoporous gold structure comprising a plurality of ligaments, and a plurality of oxide particles deposited on the nanoporous gold structure; the oxide particles are characterized by a crystalline phase. 1. A method , comprising:depositing oxide nanoparticles on a nanoporous gold support to form an active structure; andfunctionalizing the deposited oxide nanoparticles.2. The method as recited in claim 1 , the depositing comprising one or more of atomic layer deposition claim 1 , liquid phase deposition claim 1 , and wet chemical impregnation.3. The method as recited in claim 1 , the functionalizing comprising annealing the active structure at a predetermined temperature for a predetermined period of time.4. The method as recited in claim 3 , wherein the predetermined temperature is greater than 500 C claim 3 , wherein the predetermined period of time is greater than 20 min.5. The method as recited in claim 1 , further comprising etching a gold alloy to form the nanoporous gold support claim 1 , the nanoporous gold support comprising at least 99% at % gold and having a porosity of at least 50%.6. The method as recited in claim 5 , wherein the etching comprises: submersing the gold alloy in concentrated nitric acid for at least 24 hours.7. The method as recited in claim 6 , further comprising applying an electric potential to the gold alloy during the etching.8. A system claim 6 , comprisinga nanoporous gold structure comprising a plurality of ligaments; anda plurality of oxide particles deposited on the nanoporous gold structure, wherein the oxide particles are characterized by a crystalline phase.9. The system as recited in claim 8 , wherein gold in the ligaments is resistant to sintering at temperatures up to about 600 C.10. The system as recited ...

CATALYSTS, PROCESSES FOR OBTAINING AND PROCESSES FOR STEAM REFORMING

The present invention refers to processes for obtaining steam reforming catalysts containing nickel, cerium, lanthanum and copper oxides, free from potassium or alkali metals, preferably with the oxide layer being located externally with a thickness of less than 0.5 mm on the support particle, preferably the support being based on alumina, magnesium aluminate, hexaaluminates or mixtures thereof. The catalysts according to present invention show high activity, resistance to thermal deactivation and resistance to coke accumulation in the steam reforming reaction of hydrocarbons. 1. A steam reforming catalyst comprising:{'sup': '2', '#text': 'a) an inorganic oxide support selected from theta-alumina, magnesium aluminate, hexaaluminates, or a mixture thereof, having a surface area above 15 m/g; and'}b) a mixture of nickel, copper, lanthanum, and cerium oxides, with the total nickel content, expressed as nickel oxide (NiO) between 5 and 25% w/w; the copper content expressed as copper oxide (CuO) between 0.5 to 5% w/w, a Ni/(La+Ce) atomic ratio between 3 to 5 and a Ce/Al atomic ratio between 1 to 4.2. The steam reforming catalyst according to claim 1 , wherein the inorganic oxide support has a surface area above 60 m/g.3. A process for obtaining the steam reforming catalyst of claim 1 , comprising the following steps:a) preparing a solution in a polar solvent, of a nickel salt, in the form of nickel nitrate, acetate or carbonate together with copper, lanthanum, and cerium salts in the form of nitrates;b) impregnating the solution containing the nickel, copper, cerium, and lanthanum salts in an inorganic oxide support selected from theta-alumina, magnesium aluminate, hexaaluminates, or a mixture thereof, by means of the wet spot technique or by placing the support of inorganic oxide in an excess of solution to form an impregnated material; andc) drying the impregnated material in air, at a temperature ranging between 50° C. and 150° C., and for a time interval in a range ...

AGGLOMERATED ODH CATALYST

Oxidative dehydrogenation catalysts for converting lower paraffins to alkenes such as ethane to ethylene when prepared as an agglomeration, for example extruded with supports comprising slurries of NbO. 2. The agglomerated catalyst according to claim 1 , having a cumulative surface area less than 10 m/g as measured by BET and comprising less than 35 wt % of an non-antagonistic binder.3. The agglomerated catalyst according to claim 2 , having a cumulative pore volume from 0.020 to 0.20 cm3/g.4. The agglomerated catalyst according to claim 2 , having a pore size distribution less than 40% having pore width size less than 200 Angstroms.5. The agglomerated catalyst according to claim 2 , having a percent pore area distribution less than 30% and corresponding percentage of pore volume less than 10%.6. The agglomerated catalyst according to in the shape of a sphere claim 2 , rod claim 2 , ring claim 2 , or a saddle having a size from about 1.3 mm to 5 mm.7. The agglomerated catalyst according to claim 6 , wherein the NbOhydrate is acidified.8. The agglomerated catalyst according to claim 6 , wherein the NbOhydrate is treated with a base.9. The agglomerated catalyst according to claim 8 , in the shape of rods having an aspect ratio from 1 to 5/1.3 having a crush strength up to 110 N/mm.10. The agglomerated catalyst according to claim 8 , in the shape of spheres having a crush strength up to 110 N/mm.11. The agglomerated catalyst according to claim 1 , wherein the NbOhydrate is present in an amount less than 15 wt %.12. The agglomerated catalyst according to claim 1 , wherein the NbOhydrate is present in an amount greater than 15 wt %.19. The process according to claim 18 , wherein in step v) the particles are calcined at a temperature of less than 350° C.20. The process according 19 claim 18 , further comprising spheroidizing rod shaped agglomerated particles at a temperature up to 300° C. and then further calcining the resulting spheres at temperatures up to 600° C.21. ...

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

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

METHODS OF MAKING YSZ SUPPORTED CATALYST, AND METHODS OF USING THE SAME

The present invention relates to catalysts, methods of making catalysts, and methods of using catalysts, where the catalysts include: at least one of a transition metal and a transition metal oxide supported by yttria-stabilized zirconia (YSZ), where the transition metal is promoted by at least one of an alkali metal and an alkaline-earth metal. 1. A catalyst , comprising:at least one of a transition metal and a transition metal oxide supported by yttria-stabilized zirconia (YSZ), wherein the transition metal is promoted by at least one of an alkali metal and an alkaline-earth metal.2. The catalyst of claim 1 , wherein the YSZ is a porous YSZ tube.3. The catalyst of claim 1 , wherein the at least one of the transition metal and the transition metal oxide is ruthenium (Ru).4. The catalyst of claim 3 , wherein the at least one of the alkali metal and the alkaline-earth metal is barium (Ba).5. The catalyst of claim 3 , wherein the at least one of the alkali metal and the alkaline-earth metal is cesium (Cs).6. The catalyst of claim 1 , the at least one of the transition metal and the transition metal oxide is partially reduced.7. The catalyst of claim 3 , wherein the Ru is supported on Ba-modified and potassium (K)-modified zirconium dioxide (ZrO).8. The catalyst of claim 3 , wherein the Ru is alloyed with the yttrium of the YSZ.9. The catalyst of claim 3 , wherein the YSZ is a porous tube comprising an outside diameter of about 1 cm and a wall thickness of about 0.134 cm.10. The catalyst of claim 3 , wherein the porous tube comprises about 4% yttrium oxide (YO) and about 96% zirconium dioxide (ZrO).11. The catalyst of claim 3 , wherein a (Brunauer claim 3 , Emmett and Teller) BET surface area of the YSZ is about 2.24 mg.12. A method of making a catalyst claim 3 , comprising:providing a support comprising a porous tube yttria-stabilized zirconia (YSZ);loading at least one of a transition metal and a transition metal oxide onto the support using wet impregnation; ...

CATALYST EFFECTIVE IN THE OXIDATIVE CONVERSION OF ETHYLENE TO ETHYLENE OXIDE

The present invention provides a catalyst effective in the oxidative conversion of ethylene to ethylene oxide, comprising an alumina support and 20 to 45%by weight of the catalyst, of silver applied to the support, the catalyst meeting the following limitations (i) to (v): (i) an amount of cesium c(Cs) in mmol per Kg of catalyst of at least 2; (ii) an amount of rhenium c(Re) in mmol per Kg of catalyst of at least 3.0; (iii) an amount of tungsten c(W) in mmol per Kg of catalyst of at least 1.6; (iv) a silicon to alkaline earth metal molar ratio x of not higher than 1.80; (v) c(Cs)−c(Re)−c(W)≤4·x−0.5. 1. A catalyst effective in the oxidative conversion of ethylene to ethylene oxide , comprising an alumina support and 20 to 45% by weight of the catalyst , of silver applied to the support , the catalyst meeting the following limitations (i) to (v):(i) an amount of cesium c(Cs) in mmol per Kg of catalyst of at least 2;(ii) an amount of rhenium c(Re) in mmol per Kg of catalyst of at least 3.0;(iii) an amount of tungsten c(W) in mmol per Kg of catalyst of at least 1.6;(iv) a silicon to alkaline earth metal molar ratio x of not higher than 1.80;(v) c(Cs)−c(Re)−c(W)≤4·x−0.5.2. The catalyst according to claim 1 , wherein{'br': None, 'i': c', 'c', 'c', 'x−, '(Cs)−(Re)−(W)≤4·1.3.'}3. The catalyst according to claim 2 , wherein{'br': None, 'i': c', 'c', 'c', 'x−, '(Cs)−(Re)−(W)≤2.35·1.3.'}4. The catalyst according to claim 1 , wherein x is 0.1 to 1.46 claim 1 , preferably 0.1 to 1.10.5. The catalyst according to claim 1 , whereinc(Cs) is 4.5 to 11.3; and/orc(Re) is 3.0 to 9; and/orc(W) is 1.6 to 5.5.6. The catalyst according to claim 1 , comprising an amount of potassium c(K) in mmol per Kg of catalyst of 2.6 to 10.3.7. The catalyst according to claim 1 , comprising an amount of sodium c(Na) in mmol per Kg of catalyst of 0.2 to 10.8.8. The catalyst according to claim 1 , comprising an amount of lithium c(Li) in mmol per Kg of catalyst of 43 to 86.9. The catalyst according to ...

Process for Production of Attrition Stable Granulated Material

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

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

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

SUPPORTED CATALYST AND METHOD OF PRODUCING FIBROUS CARBON NANOSTRUCTURES

A supported catalyst comprises: a support that is particulate; and a composite layer laminate formed outside the support and including two or more composite layers, wherein each of the composite layers includes a catalyst portion containing a catalyst and a metal compound portion containing a metal compound, the support contains 10 mass % or more of each of Al and Si, and a volume-average particle diameter of the support is 50 μm or more and 400 μm or less. 1. A supported catalyst , comprising:a support that is particulate; anda composite layer laminate formed outside the support,wherein the composite layer laminate is composed of n composite layers, where n is an integer of 2 or more,each of the composite layers in the composite layer laminate includes a catalyst portion containing a catalyst and a metal compound portion containing a metal compound,the support contains 10 mass % or more of each of Al and Si, anda volume-average particle diameter of the support is 50 μm or more and 400 μm or less.2. The supported catalyst according to claim 1 ,wherein the metal compound portion contains 10 mass % or more of Al.3. The supported catalyst according to claim 1 ,wherein the catalyst portion contains at least metal of any of Fe, Co, and Ni.4. The supported catalyst according to any one of claim 1 ,wherein the composite layer in the composite layer laminate includes a metal compound layer which is the metal compound portion in layer form, a catalyst layer which is the catalyst portion in layer form, and/or a mixed layer in which the metal compound and the catalyst coexist.5. The supported catalyst according to claim 4 ,wherein a catalyst metal equivalent thickness of the catalyst contained in the composite layer is 0.1 nm or more and 10 nm or less per one composite layer.6. The supported catalyst according to claim 4 ,wherein a metal compound equivalent thickness of the metal compound contained in the composite layer is 1 nm or more and 1 μm or less per one composite layer ...

METHOD FOR PRODUCING A CATALYST FOR THE PARTIAL OXIDATION/AMMOXIDATION OF OLEFINS

The present invention relates to a method for producing a supported catalyst, a catalyst which is obtainable using the method, and use thereof for the partial oxidation or ammoxidation of olefins, in particular for the oxidation of propene to acrolein, of isobutene to methacrolein, and/or the ammoxidation of propene to acrylonitrile. The method according to the invention includes the following steps: a) providing a solution in which precursor compounds of the catalytically active component are essentially completely dissolved in a suitable solvent; b) bringing the solution obtained in step a) into contact with a (chemically) inert, porous support having a specific surface of 1 to 500 m/g; c) heat treatment of the material obtained in step b), in which the precursor compounds of the catalytically active component are converted to their oxides. 1. Method for producing a catalyst which includes as the catalytically active component a compound having the general formula MoBiFeABCDO , where A stands for Ni and/or Co , B stands for one or more metals selected from Mg , Cr , Mn , Zn , Ce , and Ca and combinations thereof , C stands for W , and D stands for one or more alkali metals , where x stands for a number from 10 to 14 , y stands for a number from 0.1 to 5 , z stands for a number from 0.5 to 5 , a stands for a number from 1 to 10 , b stands for a number from 0.1 to 6 , c stands for a number from ≧0 to 2 , d stands for a number from 0.02 to 2 , and v is determined by the oxidation state of the elements , the method including the following steps:a) Providing a solution in which precursor compounds of the catalytically active component are essentially completely dissolved in a suitable solvent;{'sup': '2', 'b) Bringing the solution obtained in step a) into contact with a chemically inert, porous support having a specific surface of 1 to 500 m/g;'}c) Heat treatment of the material obtained in step b), in which the precursor compounds of the catalytically active component ...

METHOD FOR MANUFACTURING RUTHENIUM OXIDE-SUPPORTED CATALYST FOR PREPARING CHLORINE AND CATALYST MANUFACTURED THEREBY

The present invention relates to a method for manufacturing a ruthenium oxide-supported catalyst for preparing chlorine, and more particularly, to a method for manufacturing a catalyst and a catalyst manufactured thereby, wherein the catalyst includes a ruthenium ingredient of which a support level on an outer surface of a support is significantly improved, and the use of the catalyst in preparing chlorine can provide a high conversion rate of chlorine even at a low reaction temperature. According to an embodiment of the present invention, the method for manufacturing a ruthenium oxide-supported catalyst for preparing chlorine may include the steps of: (a) dissolving a ruthenium compound in an organic solvent to prepare a solution and supporting the same on at least one support selected from titania and alumina; (b) performing drying thereon after the supporting; and (c) performing calcining thereon after the drying. According to an embodiment of the present invention, in particular, it is possible to provide a simplified process by manufacturing a catalyst including ruthenium oxide only at each outer surface layer of a titania support without alkali pretreatment, thereby exhibiting an advantageous effect in terms of scale-up. 1. A method for manufacturing a ruthenium oxide-supported catalyst for preparing chlorine , the method comprising the steps of:(a) dissolving a ruthenium compound in an organic solvent to prepare a solution and supporting the same on at least one support selected from titania and alumina;(b) performing drying thereon after the supporting; and(c) performing calcining thereon after the drying.2. The method of claim 1 , wherein the organic solvent in the step (a) is monoalcohol.3. The method of claim 2 , wherein the monoalcohol is a primary alcohol of C3 or higher.4. The method of claim 1 , wherein the titanium support in the step (a) has a specific surface area of 5-300 m/g.5. The method of claim 1 , wherein the drying in the step (b) is ...

Mixed Metal Oxide Catalyst useful for Paraffin Dehydrogenation

A catalyst, methods of making, and process of dehydrogenating paraffins utilizing the catalyst. The catalyst includes at least 20 mass % Zn, a catalyst support and a catalyst stabilizer. The catalyst is further characterizable by physical properties such as activity parameter measured under specified conditions. The catalyst may also be disposed on a porous support in an attrition-resistant form and used in a fluidized bed reactor. 1. A mixed metal oxide catalyst suitable for the dehydrogenation of paraffins having 2-8 carbon atoms , comprising a catalyst composition of the general formula (AC) (CS) (ST) whereina) AC (Active Catalyst) represents oxides of zinc (Zn) wherein the catalyst comprises at least 20 mass % Zn,b) CS (Catalyst Support) represents oxides of aluminum (Al), silicon (Si), and titanium (Ti) or mixtures thereof,c) ST (Support Stabilizer) represents oxides of metals selected from the group of cerium (Ce), dysprosium (Dy), erbium (Er), europium (Eu), gadolinium (Gd), lanthanum (La), neodymium (Nd), praseodymium (Pr), samarium (Sm), terbium (Tb), ytterbium (Yb), yttrium (Y), tungsten (W), zirconium (Zr), or mixtures thereof, andcharacterizable by a Activity Parameter >90,000, Selectivity Parameter <0.5 and a stability parameter <0.005 using a test where the mixed metal oxide catalyst is loaded in a fixed-bed reactor such that the 50>dT/dP>10 (diameter of tube to diameter of catalyst particles) and 200>L/dP>50 (length of catalyst bed to diameter of catalyst particles) and 2>dP>0.5 mm exposed to a feed stream of propane at a temperature of 650oC, atmospheric pressure and a feed rate of 10 hr−1 weight hourly space velocity.2. The catalyst composition according to wherein the catalyst is characterizable by an activity parameter of between 90 claim 1 ,000 and about 125 claim 1 ,000 using a test where the mixed metal oxide catalyst is loaded in a fixed-bed reactor such that the 50>dT/dP>10 (diameter of tube to diameter of catalyst particles) and 200>L/dP>50 ...

ORGANIC MATERIAL DECOMPOSITION CATALYST AND ORGANIC MATERIAL DECOMPOSITION APPARATUS

An organic material decomposition catalyst that contains BaCOand a perovskite composite oxide represented by ABMO, wherein A contains Ba, B contains Zr, and M denotes Mn. A peak intensity I(BaCO(111)) of BaCO(111) of the BaCOand a peak intensity I(BaZrO(110)) of a perovskite composite oxide ABMO(110) of the perovskite composite oxide represented by ABMO, each determined by X-ray diffractometry of the organic material decomposition catalyst, have a ratio I(BaCO(111))/I(BaZrO(110)) in a range of 0.022 to 0.052. In another aspect, in the perovskite composite oxide represented by ABMO, 1.01≤x≤1.06, 0.1≤z≤0.125, and y+z=1 are satisfied, w denotes a positive value that satisfies electroneutrality, and the organic material decomposition catalyst has a specific surface area in the range of 12.3 to 16.9 m/g. 1. An organic material decomposition catalyst , comprising:{'sub': '3', '#text': 'BaCO; and'}{'sub': ['x', 'y', 'z', 'w'], '#text': 'a perovskite composite oxide represented by ABMO, wherein A contains Ba, B contains Zr, and M denotes Mn,'}{'sub': ['3', '3', '3', '3', 'x', 'y', 'z', 'w', 'x', 'y', 'z', 'w', '3', '3'], '#text': 'wherein a peak intensity I(BaCO(111)) of BaCO(111) of the BaCOand a peak intensity I(BaZrO(110)) of a perovskite composite oxide ABMO(110) of the perovskite composite oxide represented by ABMO, each determined by X-ray diffractometry of the organic material decomposition catalyst, have a ratio I(BaCO(111))/I(BaZrO(110)) in a range of 0.022 to 0.052.'}2. The organic material decomposition catalyst according to claim 1 , wherein the organic material decomposition catalyst has a specific surface area in a range of 12.3 to 16.9 m/g.3. The organic material decomposition catalyst according to claim 2 , wherein the ratio I(BaCO(111))/I(BaZrO(110)) ranges from 0.022 to 0.041.4. The organic material decomposition catalyst according to claim 3 , wherein the organic material decomposition catalyst has a specific surface area in the range of 12.3 to 13.5 m/g. ...

CATALYSTS COMPRISING A ZIRCONIA AND GALLIUM OXIDE COMPONENT FOR PRODUCTION OF C2 TO C4 OLEFINS

A process for preparing Cto Colefins includes introducing a feed stream comprising hydrogen gas and a carbon-containing gas selected from carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor. The feed stream is converted into a product stream including Cto Colefins in the reaction zone in the presence of the hybrid catalyst. The hybrid catalyst includes a metal oxide catalyst component comprising gallium oxide and phase pure zirconia, and a microporous catalyst component. 1. A process for preparing Cto Colefins comprising:introducing a feed stream comprising hydrogen gas and a carbon-containing gas selected from the group consisting of carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor; and{'sub': 2', '4, 'claim-text': a metal oxide catalyst component comprising gallium oxide and phase pure zirconia; and', 'a microporous catalyst component., 'converting the feed stream into a product stream comprising Cto Colefins in the reaction zone in the presence of a hybrid catalyst, the hybrid catalyst comprising2. The process of claim 1 , wherein the phase pure zirconia comprises crystalline phase pure zirconia.3. The process of claim 1 , wherein the phase pure zirconia comprises monoclinic phase pure zirconia.4. The process of claim 1 , wherein the phase pure zirconia has a BET surface area that is greater than or equal to 40 m/g.5. The process of claim 1 , wherein the phase pure zirconia has a BET surface area that is greater than or equal to 100 m/g.6. The process of claim 1 , wherein the metal oxide catalyst component comprises from greater than 0.0 g gallium per 100 g phase pure zirconia to 30.0 g gallium per 100 g of phase pure zirconia.7. The process of claim 1 , wherein the metal oxide catalyst component comprises from greater than 0.0 g gallium per 100 g phase pure zirconia to 15.0 g gallium per 100 g of phase pure zirconia.8. The process of claim 1 , wherein microporous catalyst component ...

PROCESS FOR PREPARING POROUS IRON OXIDE-ZIRCONIA COMPOSITE CATALYST, POROUS IRON OXIDE-ZIRCONIA COMPOSITE CATALYST PREPARED THEREBY, AND METHOD FOR PRODUCING ALCOHOL USING THE CATALYST

The present invention relates to a porous iron oxide-zirconia composite catalyst, a preparation method thereof, and a method for producing alcohol using the same, and the iron oxide-zirconia composite catalyst having a porous structure may produce alcohol at low cost by carrying out an excellent methane reforming reaction even under room temperature and room pressure conditions through an electrochemical reaction. 1. A method for preparing a porous iron oxide-zirconia composite catalyst , the method including:impregnating a polymer template mold with a precursor mixture of iron oxide precursor and a zirconia precursor;drying the polymer template mold impregnated with the precursor mixture; andsintering the dried polymer template mold.2. The method of claim 1 ,wherein the iron oxide precursor is one or more selected from the group consisting of iron (III) nitrate, iron (III) chlorate, and iron (III) sulfate.3. The method of claim 1 ,wherein the zirconia precursor is one or more selected from the group consisting of zirconium oxynitrate, zirconium nitrate, and zirconium sulfate.4. The method of claim 1 ,wherein the iron oxide precursor and the zirconia precursor are mixed at a molar ratio of 8:1 to 2:1.5. The method of claim 1 ,wherein the polymer template mold includes a spherical polymer arranged in a face centered cubic (fcc) structure.6. The method of claim 1 ,wherein the polymer template mold is manufactured by a method including emulsion polymerization of monomers, followed by drying step.7. The method of claim 1 ,wherein the polymer template mold includes one or more polymers selected from the group consisting of poly(methyl methacrylate) [PMMA], poly(butyl methacrylate) [PBMA], poly(methyl methacrylate)(butyl methacrylate), poly(hydroxyethyl methacrylate) [PHEMA], and polystyrene.8. A porous iron oxide-zirconia composite catalyst manufactured by a method comprising:impregnating a polymer template mold with a precursor mixture of iron oxide precursor and a ...

CATALYSTS FOR THE REFORMING OF GASEOUS MIXTURES

Pyrochlore-based solid mixed oxide materials suitable for use in catalysing a hydrocarbon reforming reaction are disclosed, as well as methods of preparing the materials, and their uses in hydrocarbon reforming processes. The materials contain a catalytic quantity of inexpensive nickel and exhibit catalytic properties in dry reforming reactions that are comparable—if not better—than those observed using expensive noble metal-containing catalysts. Moreover, the Pyrochlore-based solid mixed oxide materials can be used in low temperature dry reforming reactions, where other catalysts would become deactivated due to coking. Accordingly, the catalytic materials represent a sizeable development in the industrial-scale reforming of hydrocarbons. 1. A solid mixed oxide material suitable for use in catalysing a methane dry reforming reaction , wherein the solid mixed oxide material comprises a first crystalline phase , the first crystalline phase being attributable to a pyrochlore crystal structure , and wherein the solid mixed oxide material comprises 3.5-25.0% of nickel by weight relative to the total weight of the solid mixed oxide material.2. The solid mixed oxide material of claim 1 , wherein the solid mixed oxide material comprises 5.0-25.0% of nickel by weight relative to the total weight of the solid mixed oxide material.3. The solid mixed oxide material of or claim 1 , wherein the solid mixed oxide material comprises 7.5-20.0% of nickel by weight relative to the total weight of the solid mixed oxide material.4. The solid mixed oxide material of any one of claim 1 , or claim 1 , wherein the solid mixed oxide material comprises 9.0-15.0% of nickel by weight relative to the total weight of the solid mixed oxide material.5. The solid mixed oxide material of any preceding claim claim 1 , wherein the first crystalline phase has a composition according to general formula (I) shown below{'br': None, 'sub': 2', '2', '7, 'ABO\u2003\u2003 (I)'} A is at least one trivalent ...

SOLID ACID CATALYST, PREPARATION THEREFOR AND USE THEREOF

A solid acid catalyst has a macropore specific volume of about 0.30-0.50 ml/g, a ratio of macropore specific volume to specific length of catalyst particles of about 1.0-2.5 ml/(g·mm), and a ratio of specific surface area to length of catalyst particles of about 3.40-4.50 m/mm. The macropore refers to pores having a diameter of more than 50 nm. An alkylation catalyst is based on the solid acid catalyst and can be used in alkylation reactions. The solid acid catalyst and alkylation catalyst show an improved catalyst service life and/or trimethylpentane selectivity when used in the alkylation of isoparaffins with olefins. 1. A solid acid catalyst , having a macropore specific volume in a range of about 0.30-0.50 ml/g , preferably about 0.30-0.40 ml/g , more preferably at least about 0.35 ml/g; a ratio of macropore specific volume to specific length of catalyst particles in a range of about 1.0-2.5 ml/(g·mm) , preferably about 1.1-1.8 ml/(g·mm); a ratio of specific surface area to length of catalyst particles in a range of about 3.40-4.50 m/mm , wherein the macropore refers to pores having a diameter of greater than 50 nm.2. The solid acid catalyst according to claim 1 , wherein the solid acid catalyst further has one or more of the following characteristics:a specific length of catalyst particles in a range of about 0.15-0.4 mm, preferably about 0.18-0.36 mm, more preferably about 0.20-0.32 mm;a total pore specific volume of at least about 0.40 ml/g, preferably at least about 0.45 ml/g; and{'sup': 2', '2, 'a specific surface area of not less than about 500 m/g, preferably not less than about 550 m/g.'}3. The solid acid catalyst according to claim 1 , wherein the solid acid catalyst comprises a solid acid component and a matrix material claim 1 , and wherein claim 1 , based on the total weight of the solid acid component and the matrix material claim 1 , the solid acid catalyst comprises about 2-98 wt % of the solid acid component and about 2-98 wt % of the matrix ...

METHOD FOR PRODUCING POROUS BODIES WITH ENHANCED PROPERTIES

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

SALT-FREE PRODUCTION OF METHIONINE FROM METHIONINE NITRILE

The invention refers to the use of a particulate catalyst containing 60.0 to 99.5 wt. % ZrOstabilised with an oxide of the element Hf and at least one oxide of the element M, wherein M=Ce, Si, Ti, or Y, for the hydrolysis reaction of methionine amide to methionine, wherein the median particle size xof the particulate catalyst is in the range of from 0.8 to 9.0 mm, preferably of from 1.0 to 7.0 mm. The invention also refers to a process for preparing methionine comprising a step of contacting a solution or suspension comprising methionine amide and water with said particulate catalyst to provide a reaction mixture comprising methionine and/or its ammonium salt from which methionine can be isolated. 1. A method of catalyzing the hydrolysis reaction of methionine amide to methionine , the method comprising contacting a solution or suspension comprising methionine amide and water with a particulate catalyst to produce a reaction mixture comprising methionine ,wherein the particulate catalyst comprises:{'sub': '2', '#text': '60.0 to 99.5 wt. % ZrO;'}an oxide of the element Hf; andat least one oxide of the element M, wherein M=Ce, Si, Ti, or Y,{'sub': '2', '#text': 'wherein the ZrOis stabilized by the oxide of the element Hf and the at least one oxide of the element M, and'}{'sub': '50', '#text': 'wherein the median particle size xof the particulate catalyst is in the range of from 0.8 to 9.0 mm.'}2. The method of claim 1 , wherein the element M=Si claim 1 , Ti claim 1 , or Y.3. The method of claim 1 , wherein the particle size xof the particulate catalyst is in the range of from 0.5 to 8.0 mm.4. The method of claim 1 , wherein the particulate catalyst comprises 0.1 to 40 wt. % of oxides of the elements Hf claim 1 , Ce claim 1 , Si claim 1 , Ti claim 1 , and Y.5. The method of claim 1 , wherein the particulate catalyst comprises:{'sub': ['2', '2', '2', '2', '3', '2'], '#text': '0.5 to 3.0 wt. % HfOand at least one selected from the group consisting of 0.1 to 40 wt. % TiO, ...

Organic matter decomposition catalyst, organic matter decomposition aggregate, and organic matter decomposition apparatus

An organic matter decomposition catalyst that contains a perovskite type complex oxide represented by A x B y M z O w , wherein A contains 90 at % or more of at least one element selected from the group consisting of Ba and Sr, B contains 80 at % or more of Zr, M is at least one element selected from the group consisting of Mn, Co, Ni, and Fe, y+z=1, x>1, z<0.4, and w is a positive value that satisfies electrical neutrality.

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

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

SPINEL SUPPORTED METAL CATALYST FOR STEAM REFORMING

The invention relates to a catalyst useful in the steam reforming of hydrocarbons and oxygenated hydrocarbons. The invention provides a method for preparing a catalyst comprising heating a spinel of formula ANiFeCrOwhere A is Mn or Mg and x is from 0 to 0.75 under reducing conditions at a temperature of from 800 to 1500° C., and catalysts obtainable by said method. 18-. (canceled)9. A method for preparing a catalyst comprising heating a spinel of formula ANiFeCrOwhere A is Mn or Mg and x is from >0 to 0.75 under reducing conditions at a temperature of from 800 to 1500° C. so as to cause a restructuring of the spinel to form a catalyst comprising a porous spinel phase supporting metal particles of Ni , Fe , mixtures thereof and/or alloys thereof.101. The method according to claim , wherein the spinel of formula ANiFeCrOis single phase.111. The method according to claim , wherein when A is Mn , x is less than or equal to 0.55.121. The method according to claim , wherein the metal particles have a particle size of 10 nm to 5 μm.131. A catalyst obtainable by the method of claim .14. A method of steam reforming a hydrocarbon or an oxygenated hydrocarbon comprising contacting said hydrocarbon or oxygenated hydrocarbon with steam and the catalyst according to .15. A method according to claim 14 , wherein said oxygenated hydrocarbon is steam reformed.16. A method according to claim 14 , wherein said oxygenated hydrocarbon is glycerol. The invention relates to a catalyst for the steam reforming of hydrocarbons and oxygenated hydrocarbons. The catalyst comprises Fe/Ni supported on a porous spinel lattice. In particular, the invention relates to a method for preparing said catalyst and a method of steam reforming hydrocarbons or oxygenated hydrocarbons using said catalyst.The steam reforming of natural gas (methane) is the most common method of producing commercial bulk hydrogen. There is interest in producing hydrogen from methane and other hydrocarbons for use in fuel cells. ...

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

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

PLATINUM-SULFUR-BASED SHELL CATALYST, PRODUCTION AND USE THEREOF IN THE DEHYDROGENATION OF HYDROCARBONS

The invention relates to the use of a supported, platinum-containing and sulfur-containing shell catalyst for the partial or complete dehydrogenation of perhydrogenated or partially hydrogenated cyclic hydrocarbons. The present invention also relates to a method for producing a platinum-containing and sulfur-containing shell catalyst and to a platinum-containing and sulfur-containing shell catalyst. The present invention further relates to a method for the partial or complete dehydrogenation of perhydrogenated or partially hydrogenated cyclic hydrocarbons. 2. The use as claimed in claim 1 , wherein the perhydrogenated or partly hydrogenated cyclic hydrocarbon is selected from the group consisting of cyclohexane claim 1 , methylcyclohexane claim 1 , decalin claim 1 , perhydrogenated or partly hydrogenated benzyltoluene claim 1 , perhydrogenated or partly hydrogenated N-alkylated carbazole claim 1 , especially perhydrogenated or partly hydrogenated N-ethylcarbazole claim 1 , and perhydrogenated or partly hydrogenated dibenzyltoluene and isomers thereof.3. The use as claimed in or claim 1 , wherein the dehydrogenation is performed continuously in a reactor selected from a fixed bed reactor claim 1 , a flow bed reactor or a fluidized bed reactor claim 1 , and preferably in a fixed bed reactor.4. The use as claimed in claim 1 , or claim 1 , wherein the dehydrogenation is effected at a temperature in the range from 200° C. to 400° C. claim 1 , more preferably at a temperature in the range from 230° C. to 330° C. claim 1 , especially at a temperature in the range from 260° C. to 310° C. claim 1 , and preferably at a pressure in the range of 1-5 bar claim 1 , more preferably in the range of 2-4 bar claim 1 , especially at a pressure of about 3 bar.5. The use as claimed in any of to claim 1 , wherein the shell catalyst has an outer shell including 85% by weight or more claim 1 , preferably 90% by weight or more claim 1 , especially 95% by weight or more claim 1 , of the ...

YTTRIUM-CONTAINING CATALYST FOR HIGH-TEMPERATURE CARBON DIOXIDE HYDRATION, COMBINED HIGH-TEMPERATURE CARBON DIOXIDE HYDRATION, AND REFORMING AND/OR REFORMING, AND A METHOD FOR HIGH-TEMPERATURE CARBON DIOXIDE HYDRATION, COMBINED HIGH-TEMPERATURE CARBON DIOXIDE HYDRATION AND REFORMING AND/OR REFORMING

The invention relates to a process for producing a catalyst for the high-temperature processes (i) carbon dioxide hydrogenation, (ii) combined high-temperature carbon dioxide hydrogenation and reforming and/or (iii) reforming of hydrocarbon-comprising compounds and/or carbon dioxide and the use of the catalyst of the invention in the reforming and/or hydrogenation of hydrocarbons, preferably methane, and/or of carbon dioxide. To produce the catalyst, an aluminum source, which preferably comprises a water-soluble precursor source, is brought into contact with an yttrium-comprising metal salt solution, dried and calcined. The metal salt solution comprises, in addition to the yttrium species, at least one element from the group consisting of cobalt, copper, nickel, iron and zinc. 1. A catalyst precursor , comprising at least one crystalline material which comprises yttrium and aluminum and has the characteristic that it has a cubic garnet structure , where the catalyst precursor comprises Cu , Zn , Fe , Co and/or Ni and where part of the yttrium and/or aluminum species in the crystalline material is replaced by at least one element selected from the group consisting of Cu , Zn , Ni , Co , and Fe , where a proportion of secondary phases is in the range from 0-49% by weight.2. The catalyst precursor according to claim 1 , wherein the yttrium content is in the range 15-80 mol % and the aluminum content is in the range 10-90 mol % claim 1 , where the total content of elements selected from the group consisting of Cu claim 1 , Zn claim 1 , Ni claim 1 , Co claim 1 , Fe is in the range of 0.01-10 mol %.3. The catalyst precursor according to claim 1 , wherein the catalyst precursor comprises claim 1 , in addition to a main phase cubic garnet structure claim 1 , at least one secondary phase present in a proportion in the range of 1-49% by weight.4. The catalyst precursor according to claim 1 , wherein the catalyst precursor has a BET surface area which is greater than 2 m2/g.5. ...

STABILIZATION OF BULK CATALYSTS WITH ORGANO-METALLOXANE FRAMEWORK

Bulk metallic catalyst precursor compositions are provided that include a Group VIB metal, a Group VIII metal, an organic-compound based component, and an organo-metalloxane polymer or gel. The catalyst precursor compositions can further include a binder. Amorphous sulfided catalysts formed from the catalyst precursor compositions are also provided. The catalyst precursor compositions can have a surface area of about 20 m/g or less. 1. A bulk metallic catalyst precursor composition comprising:a Group VIII metal;a Group VIB metal, a combined amount of Group VIII metal and Group VIB metal being about 1 wt % to about 80 wt % on a metal oxide basis;about 10 wt % to about 60 wt % of an organic compound-based component, the organic compound-based component is based on at least one organic complexing agent; andabout 1 wt % to about 50 wt % of an organo-metalloxane polymer, organo-metalloxane gel, or combination thereof,{'sup': '2', 'the catalyst precursor composition having a surface area of 20 m/g or less based on BET.'}2. The bulk metallic catalyst precursor composition of claim 1 , wherein the catalyst precursor composition comprises at least about 5 wt % of the organo-metalloxane polymer claim 1 , organo-metalloxane gel claim 1 , or combination thereof.3. The bulk metallic catalyst precursor composition of claim 1 , wherein the organic compound-based component is further based on organic functional groups from the organo-metalloxane polymer claim 1 , organo-metalloxane gel claim 1 , or combination thereof.4. The bulk metallic catalyst precursor composition of claim 1 , wherein the organo-metalloxane polymer claim 1 , organo-metalloxane gel claim 1 , or combination thereof is water soluble.5. The bulk metallic precursor composition of claim 1 , wherein the organo-metalloxane polymer claim 1 , organo-metalloxane gel claim 1 , or combination thereof comprises an organo-siloxane claim 1 , an organo-alumoxane claim 1 , an organo-titanoxane claim 1 , or a combination thereof ...

CHA TYPE ZEOLITIC MATERIALS AND METHODS FOR THEIR PREPARATION

The present disclosure relates to a process for the preparation of a zeolitic material having a CHA-type framework structure comprising YOand XO, wherein the process comprises: 116-. (canceled)17. A process for preparing a zeolitic material having a CHA-type framework structure comprising YOand XO , wherein the process comprises:{'sub': 2', '2', '3, 'sup': 1', '2', '3', '4', '+', '5', '6', '7', '8', '+, 'providing a mixture comprising one or more sources for YO, one or more sources for XO, one or more tetraalkylammonium cation RRRRN-containing compounds, and one or more tetraalkylammonium cation RRRRN-containing compounds as structure directing agent;'}crystallizing the mixture to obtain a zeolitic material having a CHA-type framework structure;wherein Y is a tetravalent element and X is a trivalent element,{'sup': 1', '2', '3', '5', '6', '7, 'wherein R, R, R, R, R, and Rare each independently chosen from alkyl,'}{'sup': '4', 'sub': n', '2n, 'wherein Ris chosen from CHOH and n ranges from 1 to 6, and'}{'sup': '8', 'wherein Ris chosen from cycloalkyl.'}18. The process of claim 17 , wherein R claim 17 , R claim 17 , R claim 17 , R claim 17 , R claim 17 , and Rare each independently chosen from optionally branched (C-C)alkyl.19. The process of claim 17 , wherein the one or more tetraalkylammonium cation RRRRN-containing compounds comprise one or more N claim 17 ,N claim 17 ,N-tri(C-C)alkyl(C-C)cycloalkylammonium compounds.20. The process of claim 17 , wherein the one or more tetraalkylammonium cation RRRRN-containing compounds comprise one or more compounds chosen from (C-C)hydroxyalkyl-tri(C-C)alkylammonium compounds.21. The process of claim 17 , wherein Y is chosen from Si claim 17 , Sn claim 17 , Ti claim 17 , Zr claim 17 , Ge claim 17 , and mixtures thereof.22. The process of claim 17 , wherein X is chosen from Al claim 17 , B claim 17 , In claim 17 , Ga claim 17 , and mixtures thereof.23. The process of claim 17 , wherein the mixture further comprises one or more ...

PROCESS FOR PREPARING A NICKEL-BASED CATALYST, THE NICKEL-BASED CATALYST, AND USE THEREOF IN A STEAM REFORMING PROCESS

The present invention relates to a process for preparing a nickel-based catalyst promoted with aluminium compounds with increased resistance to thermal deactivation and to the nickel-based catalyst thus obtained. In addition, the present invention relates to the use of said catalyst in a steam reforming process starting from hydrocarbons for producing hydrogen or synthesis gas. 1. Process for preparing a nickel-based catalyst , comprising the step of providing a first nickel-based catalyst , either by providing a commercial nickel-based catalyst or by carrying out steps (a)-(d):a) preparing a solution of nickel salt;b) impregnating a support of one or more inorganic oxides with the solution of nickel salt;c) drying the impregnated material;d) calcining the impregnated material;and additionally comprising the steps of:e) preparing a solution of an inorganic aluminium salt;f) impregnating the first nickel-based catalyst with the solution of inorganic aluminium salt, to act as promoter,g) drying the material impregnated in step f); andh) calcining the material dried in step g),wherein steps (e) to (h) may be repeated until a content from 0.5% to 1% w/w of aluminium is reached.2. Process for preparing a nickel-based catalyst according to claim 1 , characterized in that the nickel salt is selected from nitrate claim 1 , acetate claim 1 , oxalate or carbonate.3. Process for preparing a nickel-based catalyst according to characterized in that the solution of nickel salt additionally comprises one or more elements of the lanthanide group claim 1 , preferably lanthanum or cerium.4. Process for preparing a nickel-based catalyst according to claim 1 , characterized in that the support of one or more inorganic oxides is selected from alumina claim 1 , calcium aluminates claim 1 , magnesium aluminates claim 1 , zirconium oxides claim 1 , lanthanum claim 1 , hexa-aluminates or a mixture thereof.5. Process for preparing a nickel-based catalyst according to claim 1 , characterized ...

A MOLDING COMPRISING A MIXED OXIDE COMPRISING OXYGEN, LANTHANUM, ALUMINUM, AND COBALT

A molding comprising a mixed oxide, wherein the mixed oxide comprises oxygen, lanthanum, aluminum, and cobalt, wherein in the mixed oxide, the weight ratio of cobalt relative to aluminum, calculated as elements, is at least 0.17:1. A preparation method by a dry route. Use of the molding as a catalyst for the reforming of hydrocarbons into a synthesis gas.

Synthesis of high surface area, high entropy oxides

High surface area, high entropy oxides comprising multiple metal cations in a single-phase fluorite lattice material enables intrinsic catalytic activity without platinum group metals, tunable oxygen storage capacity, and thermal stability. These properties can be obtained through a facile sol-gel synthesis to provide a low-temperature route for production of phase-pure multi-cationic oxides. The resulting materials achieved significantly higher surface area and catalytic performance, taking advantage of all the properties endowed by the various cations in the composition.

Catalyst

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

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.

PHOTOCATALYST AND PREPARATION METHOD THEREFOR

A photocatalyst, a product including a photocatalyst, and a method for preparing a photocatalyst are provided. The photocatalyst is an inorganic oxide-based photocatalyst including inorganic oxide and a ferrocene-derived iron oxide layer formed on the inorganic oxide. 1. An inorganic oxide-based photocatalyst comprising:an inorganic oxide; anda ferrocene-derived iron oxide layer formed on the inorganic oxide.2. The inorganic oxide-based photocatalyst of claim 1 , wherein iron is contained in the ferrocene-derived iron oxide layer in an amount of 0.001 to 10 wt % compared to the inorganic oxide.3. The inorganic oxide-based photocatalyst of claim 1 , wherein the ferrocene-derived iron oxide layer is obtained by performing a heat treatment process on ferrocene deposited on the inorganic oxide.4. The inorganic oxide-based photocatalyst of claim 1 , wherein the inorganic oxide includes at least one selected from the group consisting of oxides including at least one of Ti claim 1 , Zn claim 1 , Al claim 1 , and Sn.5. The inorganic oxide-based photocatalyst of claim 1 , wherein the inorganic oxide includes at least one selected from the group consisting of a bead form claim 1 , a powder form claim 1 , a rod form claim 1 , a wire form claim 1 , a needle form claim 1 , and a fiber form claim 1 , and the inorganic oxide has a size of 1 nm to 500 μm.6. The inorganic oxide-based photocatalyst of claim 1 , wherein the inorganic oxide-based photocatalyst has photoactivity in a visible light region of 400 nm or more.7. The inorganic oxide-based photocatalyst of claim 1 , wherein the inorganic oxide-based photocatalyst has photoactivity in a dry condition of 30% or less humidity.8. The inorganic oxide-based photocatalyst of claim 1 , wherein the ferrocene-derived iron oxide includes one or more of compounds represented by the following Chemical Formula 1:{'br': None, 'sub': x', 'Y', 'Z, 'FeOH\u2003\u2003[Chemical Formula 1]'}(X, Y, and Z are each selected from 0 to 3, and X and Y ...

SHELL IMPREGNATED CATALYST AND PROCESS FOR PRODUCING A SHELL IMPREGNATED CATALYST BODY

A process for producing a catalyst, comprising the steps of modifying a carrier by a first impregnation with at least one alkaline earth metal in a first metal precursor solution, the first metal precursor being decomposed to form at least one metal oxide or metal hydroxide, thereby obtaining a modified carrier. A second impregnation is carried out by incipient wetness by a second precursor solution comprising at least one metal Me in a second solution. Finally, the second precursor is decomposed, thereby obtaining a catalyst body having an enrichment of the at least one metal Me in the outer shell of the catalyst body, the metal being present in a concentration having either as an egg-shell profile or a hammock profile. 1. A process for producing a catalyst , said process comprising the steps of:providing a carrier,modifying said carrier by a first impregnation with at least one alkaline earth metal in a first metal precursor solution,decomposing the first metal precursor to form at least one metal oxide or metal hydroxide thereby obtaining a modified carrier,carrying out a second impregnation by incipient wetness by a second precursor solution comprising at least one metal Me in a second solution, anddecomposing the second precursor thereby obtaining a catalyst body having an enrichment of the at least one metal Me in the outer shell of the catalyst body, said at least one metal being present in a concentration having either an egg-shell profile and/or a hammock profile.2. A process according to claim 1 , wherein the carrier is alumina spinel and/or calcium aluminate.3. A process according to claim 1 , wherein carrier has a pore volume 200-400 ml/kg claim 1 , and/or BET surface area 2-50 m/g.4. A process according to claim 1 , comprising repeating the second impregnation one or more times.5. A process according to claim 1 , wherein the first precursor solution is a nitrate claim 1 , carbonate or hydroxide of the alkaline earth metals.6. A process according to ...

METHOD FOR PRODUCING CONDUCTIVE MAYENITE COMPOUND POWER

If a conductive mayenite compound having a large specific surface area is obtained, the usefulness thereof in respective applications is remarkably increased. A conductive mayenite compound powder having a conduction electron density of 10cmor more and a specific surface area of 5 mgor more is produced by: the following steps: (1) forming a precursor powder by subjecting a mixture of a starting material powder and water to a hydrothermal treatment; (2) forming a mayenite compound powder by heating and dehydrating the precursor powder; (3) forming an activated mayenite compound powder by heating the compound powder in an inert gas atmosphere or in a vacuum; and (4) injecting electrons into the mayenite compound through a reduction treatment by mixing the activated mayenite compound powder with a reducing agent. 1. A mayenite compound having a conduction electron concentration of 10cmor more and a specific surface area of 5 mgor more.2. The mayenite compound according to claim 1 , wherein the mayenite compound is used as a support of a transition metal catalyst.3. The mayenite compound according to claim 1 , wherein the mayenite compound is in powder form.4. The mayenite compound according to claim 1 , wherein the mayenite compound is in a cage skeleton form.5. The mayenite compound according to claim 1 , wherein the mayenite compound is activated.6. A supported metal catalyst comprising:{'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'a support comprising a conductive mayenite compound of ; and'}a transition metal catalyst supported on the conductive mayenite compound support.7. A method of synthesizing ammonia claim 1 , the method comprising:{'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'Providing a transition metal catalyst supported on the mayenite compound according to ;'}{'sub': 2', '2', '3, 'Supplying nitrogen gas (N) and hydrogen gas (H) to contact with the transition metal catalyst so as to react with each other to produce ammonia gas (NH).'} This ...

RETAINING MATERIAL FOR POLLUTION CONTROL ELEMENT, METHOD FOR MANUFACTURING THE SAME, AND POLLUTION CONTROL DEVICE

A retaining material that can sufficiently maintain the function of retaining a pollution control element in a pollution control device at high temperature. In one aspect, the retaining material has a mat shape and contains inorganic fiber material, with the retaining material containing: a surface layer containing inorganic colloid particles; and an internal region positioned further to the inside than the surface layer, impregnated with inorganic colloid particles and organic binder; wherein the surface layer contains inorganic colloid particles at a higher concentration than the internal region; and the amount of inorganic colloid particles in the internal region is 1 mass % to 10 mass % based on the total mass of the retaining material. 1. A retaining material comprising:a sheet comprising inorganic fiber material with inorganic colloid particles and organic binder essentially uniformly dispersed in the thickness direction of the sheet; anda surface layer containing inorganic colloid particles adhered so as to coat a surface of the sheet,wherein the amount of inorganic colloid particles in the sheet is 1 mass % to 10 mass % based on the total mass of the retaining material, and the surface layer contains a higher concentration of inorganic colloid particles than the sheet.2. The retaining material according to claim 1 , wherein the surface layer is adhered so as to coat opposite surfaces of the sheet.3. The retaining material according to claim 1 , wherein the amount of inorganic colloid particles per unit area of the surface layer is 1 g/mto 20 g/m.4. The retaining material according to claim 1 , wherein the amount of organic binder is 3 mass % or less based on the total mass of retaining material.5. The retaining material according to claim 1 , wherein the sheet is a needle punched molded material.6. The retaining material according to claim 1 , wherein the organic binder is an acrylic latex.7. The retaining material according to claim 1 , wherein the ...

METAL SUBOXIDE AND METHODS OF PREPARING SAME

A metal suboxide having a specific surface area of greater than or equal to about 1.5 m/g is prepared by preparing a metal suboxide precursor, and heat-treating the metal suboxide precursor. 1. A metal suboxide having a specific surface area of greater than or equal to about 1.5 m/g.2. The metal suboxide of claim 1 , wherein the specific surface area of the metal suboxide ranges from about 1.5 m/g to about 50 m/g.3. The metal suboxide of claim 1 , wherein the metal suboxide comprises carbon in an amount of less than or equal to about 1 wt % based on a total weight of the metal suboxide.4. The metal suboxide of claim 1 , wherein the metal suboxide comprises one metal selected from a transition metal claim 1 , a post-transition metal claim 1 , and a combination thereof.5. The metal suboxide of claim 1 , wherein the metal suboxide comprises one metal selected from titanium (Ti) claim 1 , zirconium (Zr) claim 1 , hafnium (Hf) claim 1 , rutherfordium (Rf) claim 1 , vanadium (V) claim 1 , niobium (Nb) claim 1 , tantalum (Ta) claim 1 , dubnium (Db) claim 1 , chromium (Cr) claim 1 , molybdenum (Mo) claim 1 , tungsten (W) claim 1 , seaborgium (Sg) claim 1 , aluminum (Al) claim 1 , gallium (Ga) claim 1 , indium (In) claim 1 , thallium (TI) claim 1 , and a combination thereof.6. The metal suboxide of claim 5 , wherein claim 5 ,the metal suboxide is a titanium suboxide, andtitanium in the titanium suboxide has an oxidation number of about +2 to about +3.9.7. The metal suboxide of claim 1 , wherein the metal suboxide has a pore.8. A catalyst claim 1 , comprising:{'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'the metal suboxide according to .'}9. An electrochemical device claim 1 , comprising:{'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'the metal oxide according to .'} This application is a divisional application of U.S. application Ser. No. 13/528,236, filed on Jun. 20, 2012, which claims priority to and the benefit of Korean Patent Application No. 10-2012-0012565 ...

Catalyst for the methanation of syngas and producer gas

Disclosed herein, inter alia, are novel nickel-ruthenium-magnesium oxide catalyst compositions and methods of making and using the same. The catalysts provide for improved methanation activity of syngas (CO+H2) and producer gas in, for example, a fixed-bed reactor. In this manner, the CO conversion and CH4 yield can be maximized in methanation reactions.

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

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

CATALYST AND METHOD FOR PREPARING LIGHT OLEFIN USING DIRECT CONVERSION OF SYNGAS

A catalyst for preparing light olefin using direct conversion of syngas is a composite catalyst and formed by compounding component I and component II in a mechanical mixing mode. The active ingredient of component I is a metal oxide; and the component II is one or more than one of zeolite of CHA and AEI structures or metal modified CHA and/or AEI zeolite. A weight ratio of the active ingredients in the component Ito the component II is 0.1-20. The reaction process has high product yield and selectivity, wherein the sum of the selectivity of the propylene and butylene reaches 40-75%; and the sum of the selectivity of light olefin comprising ethylene, propylene and butylene can reach 50-90%. Meanwhile, the selectivity of a methane side product is less than 15%. 1. A catalyst , comprising a component I and a component II , which are compounded in a mechanical mixing mode; an active ingredient of the component I being a metal oxide; the component II being a zeolite of CHA or AEI topology; wherein ,{'sub': x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'x', 'x', 'x', 'a', 'b', '(1-a-b)', 'x', 'a', 'b', '(1-a-b)', 'x, 'the metal oxide is at least one of MnO, MnCrO, MnAlO, MnZrO, MnInO, ZnO, ZnCrO, ZnAlO, ZnGaO, ZnInO, CeO, CoAlO, FeAlO, GaO, BiO, InO, InAlMnOand InGaMnO;'}{'sub': x', 'x', 'x', 'x', 'x', 'x, 'sup': '2', 'a specific surface area of MnO, ZnO, CeO, GaO, BiOand InOis 1-100 m/g;'}{'sub': a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', '(1-a)', 'x', 'a', 'b', '(1-a-b)', 'x', 'a', 'b', '(1-a-b)', 'x, 'sup': '2', 'a specific surface area of MnCrO, MnAlO, MnZrO, MnInO, ZnCrO, ZnAlO, ZnGaO, ZnInO, CoAlO, FeAlO, InAlMnO, and InGaMnOis 5-150 m/g;'}a value range of x is 0.7-3.7, and a ...

POROUS CATALYST CARRIER PARTICLES AND METHODS OF FORMING THEREOF

A method of forming a batch of porous catalytic carrier particles may include applying a precursor mixture into a shaping assembly within an application zone to form a batch of precursor porous catalytic carrier particles, drying the batch of precursor porous catalytic carrier particles within the shaping assembly to form the batch of porous catalytic carrier particles, and directing an ejection material at the shaping assembly under a predetermined force to remove the batch of porous catalytic carrier particles from the shaping assembly. The batch of porous catalytic carrier particles may have an average pore volume of at least about 0.1 cm/g. 1. A method of forming a batch of porous catalytic carrier particles , wherein the method comprises:applying a precursor mixture into a shaping assembly within an application zone to form a batch of precursor porous catalytic carrier particles;drying the batch of precursor porous catalytic carrier particles within the shaping assembly to form the batch of greenware porous catalytic carrier particles;directing an ejection material at the shaping assembly under a predetermined force to remove the batch of greenware porous catalytic carrier particles from the shaping assembly, andfiring the batch of greenware porous catalytic carrier particles to for the batch of porous catalytic carrier particles,{'sup': '3', 'wherein the batch of porous catalytic carrier particles comprises an average pore volume of at least about 0.1 cm/g.'}2. The method of claim 1 , wherein applying the precursor mixture into a shaping assembly comprises extruding the precursor mixture through a die opening and into the shaping assembly claim 1 , wherein the shaping assembly comprises an opening configured to receive the precursor mixture claim 1 , wherein the opening is defined by at least three surfaces claim 1 , wherein the opening extends through an entire thickness of a first portion of the shaping assembly claim 1 , wherein the opening extends through ...

Mixed Metal Oxide Catalyst useful for Paraffin Dehydrogenation

The invention relates to a catalyst composition suitable for the dehydrogenation of paraffins having 2-8 carbon atoms comprising zinc oxide and titanium dioxide, optionally further comprising oxides of cerium (Ce), dysprosium (Dy), erbium (Er), europium (Eu), gadolinium (Gd), lanthanum (La), neodymium (Nd), praseodymium (Pr), samarium (Sm), terbium (Tb), ytterbium (Yb), yttrium (Y), tungsten (W) and Zirconium (Zr) or mixtures thereof, wherein said catalyst composition is substantially free of chromium and platinum. The catalysts possess unique combinations of activity, selectivity, and stability. Methods for preparing improved dehydrogenation catalysts and a process for dehydrogenating paraffins having 2-8 carbon atoms, comprising contacting the mixed metal oxide catalyst with paraffins are also described. The catalyst may also be disposed on a porous support in an attrition-resistant form and used in a fluidized bed reactor. 133-. (canceled)34. A process for continuous dehydrogenating of paraffins having 2-8 carbon atoms , preferably propane or isobutane , comprising:{'sup': −1', '−1, 'contacting said paraffins with a catalyst composition at a reaction temperature of 500-800° C., a space velocity of 0.1-5 hror 0.1-1 hrand a pressure of 0.01-0.2 MPa for a reaction period in the range of 0.05 seconds to 10 minutes;'}regenerating the catalyst with an oxygen-containing gas wherein said catalyst regeneration is performed at a reaction temperature of 500-800° C., a pressure of 0.01-0.2 MPa and a regeneration period ranging from 0.05 seconds to 10 minutes;wherein the catalyst composition comprises:(a) zinc oxide with optional modifiers selected from the group of Copper, Manganese, and Niobium and a stabilized titania support, comprising: the stabilized titania support stabilized with a stabilizing element(s) comprising zirconium, tungsten, or a rare earth element or combinations thereof; and Zn; wherein the catalyst composition from 10 to 95 wt % titania, 0.1 to 25 wt % ...

CATALYST FOR A GAS SENSOR AND A CONTACT COMBUSTION TYPE GAS SENSOR HAVING THE SAME

A catalyst for a gas sensor includes a support and a core-shell type complex contained in the support. The complex includes a metal-containing core and a porous nanostructured shell. A contact combustion type gas sensor includes the catalyst. 1. A catalyst for a gas sensor comprising:a support and a core-shell type complex contained in the support,wherein the complex includes a metal-containing core and a porous nanostructured shell.2. The catalyst for a gas sensor of claim 1 , wherein the shell includes a plurality of pores having an average diameter of less than 10 nm.3. The catalyst for a gas sensor of claim 1 , wherein the shell includes at least one selected from a group consisting of silica claim 1 , zeolite and starch.4. The catalyst for a gas sensor of claim 1 , wherein the metal includes at least one selected from a group consisting of platinum (Pt) claim 1 , palladium (Pd) claim 1 , gold (Au) claim 1 , nickel (Ni) claim 1 , ruthenium (Ru) claim 1 , copper (Cu) claim 1 , and rhodium (Rh).5. The catalyst for a gas sensor of claim 1 , wherein the complex includes a lipophilic functional group on a surface of the complex.6. The catalyst for a gas sensor of claim 5 , wherein the lipophilic functional group is derived from at least one selected from a group consisting of aluminic ester and aluminum hydroxide.7. The catalyst for a gas sensor of claim 1 , wherein the complex includes the core having an average diameter of 1 to 12 nm and the shell having an average thickness of 10 to 100 nm.8. The catalyst for a gas sensor of claim 1 , wherein the support is a ceramic including at least one selected from a group consisting of aluminum (Al) claim 1 , silicon (Si) claim 1 , boron (B) claim 1 , beryllium (Be) claim 1 , tin (Sn) claim 1 , zinc (Zn) claim 1 , tungsten (W) claim 1 , Cu claim 1 , and magnesium (Mg).9. The catalyst for the gas sensor of claim 1 , wherein the Brunauer claim 1 , Emmett claim 1 , and Teller (BET) specific surface area is 50 to 300 m/g.10. The ...

POROUS SHAPED CARBON PRODUCTS

Shaped porous carbon products and processes for preparing these products are provided. The shaped porous carbon products can be used, for example, as catalyst supports and adsorbents. Catalyst compositions including these shaped porous carbon products, processes of preparing the catalyst compositions, and various processes of using the shaped porous carbon products and catalyst compositions are also provided. 1. A process for preparing a shaped porous carbon product , the process comprising:mixing a carbonaceous material and an organic binder to form a carbon-binder mixture, wherein the binder comprises: (i) a saccharide selected from the group consisting of a monosaccharide, a disaccharide, an oligosaccharide, a derivative thereof, and any combination thereof and/or (ii) a water soluble polymer;forming the carbon-binder mixture to produce a shaped carbon composite; andheating the shaped carbon composite in a heating zone to carbonize the binder thereby producing the shaped porous carbon product.2. The process of wherein the heating zone comprises at least two heating stages that are each maintained at an approximately constant temperature and the temperature of each stage differs by at least about 50° C. claim 1 , with the temperature increasing from one stage to the next.3. The process of wherein the temperature of each stage differs by from about 50° C. to about 500° C. claim 2 ,4. The process of wherein the heating zone comprises at least six heating stages that are each maintained at an approximately constant temperature and the temperature of each stage independently differs by at least about 50° C. claim 1 , from the preceding stage.59-. (canceled)10. The process of wherein the heating zone comprises a multi-stage continuous rotary kiln.11. The process of wherein the carbon-binder mixture further comprises a solvent.1215-. (canceled)16. The process of wherein the process further comprises drying the shaped carbon composite to remove at least a portion of the ...

Nickel supported catalyst for combined steam and carbon dioxide reforming with natural gas

A nickel-supported catalyst for combined steam and carbon dioxide reforming, as a catalyst which is used in a process of preparing a synthesis gas by combined steam and carbon dioxide reforming with natural gas, is provided. More particularly, in the nickel-supported catalyst, nickel is supported as an active metal on a lanthanum oxide support.

New catalyst system for producing maleic anhydride by means of the catalytic oxidation of n-butane

The invention relates to a catalyst system for producing maleic anhydride by means of the catalytic oxidation of n-butane, comprising at least one reactor tube, which has two catalyst layers consisting of different catalyst particles, characterized in that the geometric surface area per catalyst particle is greater in the catalyst layer that is first in the gas flow direction than in the second catalyst layer. The invention further relates to a process for producing maleic anhydride by means of the catalytic oxidation of n-butane, wherein a mixture of oxygen and n-butane is fed through the catalyst system according to the invention and the at least one reactor tube is at elevated temperature.

Mixed Oxides Catalysts for Oxidative Coupling of Methane

An OCM nanoplate catalyst comprising >25 wt. % nanoplates; wherein a nanoplate is a three-dimensional object defined in accordance with ISO/TS 80004-2:2015; wherein a nanoplate is characterized by a first external dimension (thickness (t)>100 nm), a second external dimension (length (l)≥t), and a third external dimension (width (w)≥t); wherein l and w can be the same or different; and wherein l≥5 t, w≥5 t, or l≥5 t and w≥5 t; and wherein the OCM nanoplate catalyst has general formula A a Z b E c D d O x ; wherein A=alkaline earth metal; Z=first rare earth element; E=second rare earth element; D=redox agent/third rare earth element; wherein the first, second, and third rare earth element are not the same; wherein a=1.0; wherein b=1.0 to 3.0; wherein c=0 to 1.5; wherein d=0 to 1.5; wherein (b>(c+d)); and wherein x balances the oxidation states.

AGGLOMERATED ODH CATALYST

Oxidative dehydrogenation catalysts for converting lower paraffins to alkenes such as ethane to ethylene when prepared as an agglomeration, for example extruded with supports comprising slurries of NbO. 127-. (canceled)28. An agglomerated catalyst , wherein the agglomerated catalyst is prepared from at least: [{'br': None, 'sub': 1.0', '0.12-0.49', '0.6-0.16', '0.15-0.20', 'd, 'MoVTeNbO'}, 'wherein d is a number to satisfy the valence of the oxide; and, '10 wt. % to 95 wt. % of a catalyst active phase of the formula{'sub': 2', '5, '5 wt. % to 90 wt. % of NbOhydrate.'}29. The agglomerated catalyst according to claim 28 , further comprising up to 80 wt. % of a non-antagonistic binder.30. The agglomerated catalyst according to claim 29 , wherein the non-antagonistic binder is chosen from oxides of aluminum claim 29 , titanium claim 29 , and zirconium.31. The agglomerated catalyst according to claim 30 , wherein the non-antagonistic binder is present in the amount of 35 wt. % to 65 wt. % based on the weight of the agglomerated catalyst and the agglomerated catalyst has a surface area up to 250 m/g.32. The agglomerated catalyst according to 30 claim 30 , wherein the oxide of aluminum is Boehmite (Al(O)OH).33. The agglomerated catalyst according to claim 30 , wherein the non-antagonistic binder is an oxide of titanium.34. The agglomerated catalyst according to claim 30 , wherein the non-antagonistic binder is an oxide of zirconium.35. The agglomerated catalyst according to claim 28 , having a cumulative surface area less than 10 m/g as measured by BET and comprising less than 35 wt % of a non-antagonistic binder.36. The agglomerated catalyst according to claim 35 , having a cumulative pore volume from 0.020 to 0.20 cm/g.37. The agglomerated catalyst according to claim 35 , having a pore size distribution less than 40% and having a pore width size less than 200 Angstroms.38. The agglomerated catalyst according to claim 35 , having a percent pore area distribution less than ...

Catalyst Complex

Embodiments relate to a method of producing a modified double metal cyanide complex, a method of producing a monol or polyol that includes providing the modified double metal cyanide complex, an alkylene oxide polymerization process that includes providing the modified double metal cyanide complex, a batch, semi-batch, or continuous manufacturing process that includes providing the modified double metal cyanide complex, and a polyether polyol prepared using the batch, semi-batch, or continuous manufacturing process that includes providing the modified double metal cyanide complex. 1. A method for producing a catalyst complex , the methodcomprising:{'sup': 2', '1', '1', '3', '1', '3', '3', '3', '3', '3, 'a) forming a starting solution comprising i) a solvent that includes at least one of water and a liquid aliphatic alcohol, the solvent having dissolved therein ii) a cyanometallate compound having an Mmetal cyanometallate group and iii) a Mmetal salt which reacts with the cyanometallate compound to form a water-insoluble Mmetal cyanometallate, which starting solution further contains 0.01 to 10 moles, per mole of cyanometallate compound, of iii) at least one Mmetal compound different from the Mmetal salt, the Mmetal compound being a compound of a Mmetal which is not titanium, the Mmetal being selected from one or more of magnesium, a Group 3-Group 15 metal other than titanium, or a lanthanide series metal which Mmetal is bonded to at least one alkoxide, aryloxy, carboxylate, acyl, pyrophosphate, phosphate, thiophosphate, dithiophosphate, phosphate ester, thiophosphate ester, amide, oxide, siloxide, hydride, carbamate or hydrocarbon anion, and the Mmetal compound is devoid of halide anions;'}{'sup': 1', '1, 'b) reacting the cyanometallate compound and Mmetal salt to form a water-insoluble catalyst complex that includes a Mmetal cyanometallate,'}2. The process of further comprising a step c) of washing the water-insoluble catalyst complex with a wash liquid comprising ...

POROUS BODIES WITH ENHANCED PORE ARCHITECTURE PREPARED WITHOUT A HIGH-TEMPERATURE BURNOUT MATERIAL

A precursor mixture for producing a porous body, wherein the precursor mixture comprises: (i) at least one milled alpha alumina powder having a particle size of 0.1 to 6 microns, (ii) non-silicate powder that functions as a binder of the alpha alumina powders, and (iii) at least one burnout material having a particle size of 1-10 microns and a decomposition temperature of less than 550° C., with the proviso that a burnout material having a decomposition temperature of 550° C. or greater is excluded from the precursor mixture. 1. A method for producing a porous body , the method comprising:providing a precursor mixture comprising (i) milled alpha alumina powder having a particle size of 0.1 to 6 microns, (ii) non-silicate binder of the alpha alumina powders, and (iii) a burnout material having a particle size of 1-10 microns and a decomposition temperature of less than 550° C., with the proviso that a burnout material having a decomposition temperature of 550° C. or above is excluded;forming the precursor mixture into a predetermined shape; andsubjecting the shape to a heat treatment step in which the shape is sintered to produce the porous body.2. The method of claim 12 , further comprising unmilled alpha alumina powder having a particle size of 10 to 100 microns in said precursor mixture.3. The method of claim 13 , wherein the weight ratio of milled to unmilled alpha alumina powder is in a range of 0.25:1 to about 5:1.4. The method of claim 12 , wherein unmilled alpha alumina powder is excluded from the precursor mixture.5. The precursor mixture of claim 12 , wherein the non-silicate binder is nano-sized boehmite6. The method of claim 12 , wherein the providing the precursor mixture comprises:(i) dispersing said non-silicate binder into water to produce a dispersion of said binder;(ii) adding said milled alpha alumina powder having a particle size of 0.1 to 6 microns to the dispersion of the non-silicate binder, and mixing until a first homogeneous mixture is ...

MULTI-LOBED POROUS CERAMIC BODY AND PROCESS FOR MAKING THE SAME

A carrier having at least three lobes, a first end, a second end, a wall between the ends and a non-uniform radius of transition at the intersection of an end and the wall is disclosed. A catalyst comprising the carrier, silver and promoters deposited on the carrier and useful for the epoxidation of olefins is also disclosed. A method for making the carrier, a method for making the catalyst and a process for epoxidation of an olefin with the catalyst are also disclosed. 1. A porous ceramic body , comprising: a first end; a second end; and a wall disposed between and intersecting said ends , said wall comprising at least three lobes and three valleys formed in the length of the wall , said lobes rounded at the intersection of said first end and said wall and said valleys not rounded at the intersection of said first end and said wall , each valley located between two of said lobes; wherein said ceramic body comprises a first radius located at the apex of a lobe and a second radius located at a nadir between two adjacent lobes and said first radius is larger than said second radius.2. The porous ceramic body of wherein said first radius is at least three times greater than said second radius. This application is a continuation of U.S. application Ser. No. 15/638,887, filed Jun. 30, 2017, granted on May 15, 2018 as U.S. Pat. No. 9,968,923, which is a continuation of U.S. application Ser. No. 14/677,090, filed Apr. 2, 2015, granted on Jul. 4, 2017 as U.S. Pat. No. 9,694,355, which is a continuation of U.S. application Ser. No. 14/524,226 filed Oct. 27, 2014, granted on Apr. 7, 2015 as U.S. Pat. No. 8,999,887, which is a divisional of U.S. application Ser. No. 13/316783 filed Dec. 12, 2011, granted on Oct. 28, 2014 as U.S. Pat. No. 8,871,677, which claims the benefit of U.S. Provisional Application No. 61/428,009 filed Dec. 29, 2010.This invention relates to porous ceramic bodies having a contoured shape that is particularly suitable for use as a carrier for ...

SELECTIVE HYDROGENATION METHODS

The present disclosure relates to methods for selectively hydrogenating acetylene, to methods for starting up a selective hydrogenation reactor, and to hydrogenation catalysts useful in such methods. In one aspect, the disclosure provides a variety of methods for starting up reactors for use in methods for selectively hydrogenating acetylene using a catalyst composition comprises a porous support, palladium, and one or more ionic liquids. 1. A method of starting up a selective hydrogenation reactor , the reactor housing one or more catalyst beds each containing a catalyst suitable for selectively hydrogenating acetylene in a process gas comprising at least 10 mol. % ethylene , at least 1 ppm acetylene , and at least 5 mol. % hydrogen , the method comprisingproviding each catalyst bed at no more than a first temperature, the catalyst of the catalyst bed being in contact with a first gas, the first gas being non-reactive in the presence of the catalyst at the first temperature;in the presence of the first gas, heating each catalyst bed to at least a second temperature, the second temperature being at least 20 degrees greater than the first temperature, the first gas being non-reactive in the presence of the catalyst at the second temperature; and thenchanging the composition of the gas in contact with the catalyst from the first gas to a flow of the process gas while the catalyst bed is at least at the second temperature; andallowing the process gas to flow through the catalyst bed until a concentration of acetylene at an outlet of the reactor is less than 1 ppm.2. The method of claim 1 , wherein the catalyst of each catalyst bed has not been contacted in the reactor with carbon monoxide in an amount in excess of 100 ppm claim 1 , and wherein the method includes refraining from adding carbon monoxide to the process gas.3. A method of starting up a selective hydrogenation reactor claim 1 , the reactor housing one or more catalyst beds each containing a catalyst ...

Selective hydrogenation methods and catalysts

The present disclosure relates to methods for selectively hydrogenating acetylene, to methods for starting up a selective hydrogenation reactor, and to hydrogenation catalysts useful in such methods. In one aspect, the disclosure provides a method for selectively hydrogenating acetylene, the method comprising contacting a catalyst composition with a process gas. The catalyst composition comprises a porous support, palladium, and one or more ionic liquids. The process gas includes ethylene, present in the process gas in an amount of at least 20 mol. %; and acetylene, present in the process gas in an amount of at least 1 ppm. At least 90% of the acetylene present in the process gas is hydrogenated, and the selective hydrogenation is conducted without thermal runaway. Notably, the process gas is contacted with the catalyst at a gas hourly space velocity (GHSV) based on total catalyst volume in one bed or multiple beds of at least 7,100 h−1.

NICKEL CONTAINING MIXED METAL-OXIDE/CARBON BULK HYDROPROCESSING CATALYSTS AND THEIR APPLICATION

The current invention relates a process for making and using a bulk catalyst precursor (i.e. no support material is added as such) comprising Ni and Mo and/or W and an organic component, wherein the molar ratio of C:(Mo+W) ranges from 1.5 to 10. The bulk catalyst precursor is prepared from a mixture of metal-precursors with an organic agent. The organic agent is partly decomposed to form a mixed metal-oxide/C phase which is in effect the bulk catalyst precursor. This bulk catalyst precursor (i) is effectively insoluble in water (ii) does not have any appreciable pore volume or surface area and (iii) does not contain a (nano)crystalline metal-oxide phase as characterized by XRD. 1. A process for hydroprocessing of a hydrocarbon feedstock comprising sulphur and nitrogen containing organic compounds comprising the step of contacting the hydrocarbon feedstock with a NiW , NiMo or NiMoW oxidic bulk catalyst obtained from a NiW , NiMo or NiMoW bulk catalyst precursor composition comprising nickel oxide , and molybdenum oxide or tungsten oxide or mixtures thereof , and an organic component prepared from an organic additive , wherein the total amount of molybdenum oxide and tungsten oxide is at least 30 wt % , the molar ratio of nickel to molybdenum plus tungsten is higher than 0.05 , the molar ratio of carbon to molybdenum plus tungsten is between 1.5 and 10; and wherein the organic additive is selected from Acetic acid , Aspartic acid , Citric acid , Formic acid , Fumaric acid , Gluconic acid , Glutamic acid , Glyoxylic acid , Ketoglutaric acid , Maleic acid , Malic acid , Oxaloacetic acid , Propionic acid , Pyruvic acid , Succinic acid , Fructose , Glucose , Lactose , Saccharose , Sorbitol , Xylitol , Serine and mixtures thereof where the bulk catalyst precursor further comprises Ni-crystals detected by transmission electron microscopy technique (TEM) , the catalyst comprising a minimum metal loading of 2.0 moles of molybdenum plus tungsten per liter reactor , wherein ...

CATALYST FOR THE PRODUCTION OF CARBOXYLIC ACID ESTER

Catalysts and methods for use in conversion of glycerides and free fatty acids to biodiesel are described. A batch or continuous process may be used with the catalysts for transesterification of triglycerides with an alkyl alcohol to produce corresponding mono carboxylic acid esters and glycerol in high yields and purity. Similarly, alkyl and aryl carboxylic acids and free fatty acids are also converted to corresponding alkyl esters. Catalysts are capable of simultaneous esterification and transesterification under same process conditions. The described catalysts are thermostable, long lasting, and highly active. 1: A catalyst comprising:at least one Mesoporous Linde Type A (MLTA) zeolite, alone or in combination with:at least one ion exchanged Modified Molecular Sieve (MMS) selected from the group consisting of MMS-3 ÅK, MMS-3 ÅCs, MMS-4 ÅK, MMS-4 ÅCs, MMS-5 ÅK and MMS-5 ÅCs; and/orat least one metal oxide selected from the group consisting of groups IIB, IIIA, IIIB, IVA and IVB metals.2: The catalyst of claim 1 , wherein the at least one metal oxide is selected from the group of consisting of Al claim 1 , Ga claim 1 , Hf claim 1 , La claim 1 , Si claim 1 , Ti claim 1 , Zn and Zr metal.3: The catalyst of claim 1 , wherein the catalyst has a composition u(AlO).v(TiO).w(ZnO).x(MMS).y(MLTA) claim 1 , wherein 0≤u≤3 (wt); 0≤v≤3 (wt); 0≤w≤3 (wt); and x+y≥0.4: The catalyst of claim 3 , wherein the catalyst has a composition 1(AlO).1(TiO).1(ZnO).12.5(MMS).4.2(MLTA) or 1(AlO).1(TiO).1(ZnO).2.3(MMS).8.3(MLTA).56-. (canceled)7: The catalyst of claim 1 , wherein the catalyst has an average pore diameter between about 10 Å and about 500 Å claim 1 , a surface area between about 1 m/g and about 100 m/g claim 1 , and/or a pore volume between about 0.01 cm/g and 1 cm/g.813-. (canceled)14: A method of performing an esterification and/or a transesterification of a starting material claim 1 , comprising reacting the starting material with an alcohol in the presence of a catalyst as ...

Selective Hydrogenation Catalyst and Methods of Making and Using Same

A method of making a selective hydrogenation catalyst comprising contacting a support with a palladium-containing compound to form a supported-palladium composition; contacting the supported-palladium composition with an organophosphorus compound and a weak acid to form a catalyst composition; and reducing the catalyst composition to form the catalyst. A method of making a selective hydrogenation catalyst comprising contacting an alumina support with a palladium-containing compound to form a supported-palladium composition; contacting the supported-palladium composition with silver nitrate and potassium fluoride to form a mixture; contacting the mixture with an organophosphorus compound and a weak acid to form a catalyst precursor; and reducing the catalyst precursor to form the catalyst. 1. A method of making a selective hydrogenation catalyst comprising:contacting a support with a palladium-containing compound to form a supported-palladium composition;contacting the supported-palladium composition with an organophosphorus compound and a weak acid to form a selective hydrogenation catalyst composition; andreducing the selective hydrogenation catalyst composition to form the selective hydrogenation catalyst.2. The method of wherein the organophosphorus compound is represented by the general formula (R)(OR′)P═O claim 1 , wherein x and y are integers ranging from 0 to 3 and x plus y equals 3 claim 1 , wherein each R is hydrogen claim 1 , a hydrocarbyl group claim 1 , or combinations thereof; and wherein each R′ is a hydrocarbyl group3. The method of wherein the organophosphorus compound comprises a phosphine oxide claim 1 , a phosphinate claim 1 , a phosphonate claim 1 , a phosphate claim 1 , or combinations thereof.4. The method of wherein the organophosphorus compound is a product of an organophosphorus compound precursor represented by the general formula of (R)(OR′)P claim 1 , wherein x and y are integers ranging from 0 to 3 and x plus y equals 3 claim 1 , wherein ...

CRUSH STRENGTH AND POROSITY OF AN ALUMINA CARRIER FOR ENHANCED VAM CATALYSTS

Disclosed is a supported catalyst for the preparation of vinyl acetate monomer, a process for preparing the supported catalyst in tablet or pellet form, and a catalytic process for the manufacturing vinyl acetate using the supported catalyst. Specifically, it is shown that catalyst performance shows a strong dependence on the crush strength of the tableted or pelletized alumina support used in the process to make the catalyst, and that the crush strength of the catalyst is closely related to the porosity of the support. Catalyst activity and selectivity can be enhanced by tailoring the crush strength of the support. 1. A process for preparing a supported catalyst , the process comprising:a) providing an alumina support in tablet form having an average crush strength of greater than about 8 lbf/mm and less than about 12 lbf/mm, a pore volume (mercury intrusion porosimetry, HgPV) from 0.25 mL/g to 0.35 mL/g, and a crystalline α-alumina content of greater than 93%;b) contacting the alumina support with a composition to provide an impregnated alumina support, the composition comprising [1] a palladium salt and a gold salt, and [2] a fixing agent selected from an alkali metal, an alkaline earth metal, or an ammonium compound of hydroxide, carbonate, bicarbonate, or metasilicate, or any combination thereof;c) calcining the impregnated alumina support in a non-reducing atmosphere for a time and a temperature sufficient to at least partially decompose the palladium salt and the gold salt; andd) reducing the calcined impregnated alumina support comprising partially decomposed palladium and gold salts with a reducing agent for a time and a temperature sufficient to provide a supported catalyst comprising palladium metal and gold metal.2. A process for preparing a supported catalyst according to claim 1 , further comprising after the contacting step claim 1 , the steps of [b1] drying the impregnated alumina support; [b2] washing the impregnated alumina support with water; and ...

HIGH PORE VOLUME ALUMINA SUPPORTED CATALYST FOR VINYL ACETATE MONOMER (VAM) PROCESS

Disclosed is a supported catalyst for the preparation of vinyl acetate monomer (VAM), a process for preparing a catalyst comprising an extruded alumina support, and a catalytic process for the manufacturing vinyl acetate using the supported catalyst. Specifically, it is shown that for activated palladium-gold VAM catalysts prepared using extruded alumina supports, enhanced performance is demonstrated with increased pore volume of the support, and the gas hourly space velocity (GHSV, hr), which was found to significantly increase the space time yield as GHSV increased as compared to the non-extruded alumina supported catalysts. 1. A process for preparing a supported catalyst , the process comprising:a) providing an extruded alumina support having a pore volume (measured by mercury intrusion porosimetry, HgPV) from 0.35 mL/g to 0.80 mL/g, and a crystalline α-alumina content of greater than 93%;b) contacting the alumina support with a composition to provide an impregnated alumina support, the composition comprising [1] a palladium salt and a gold salt, and [2] a fixing agent selected from an alkali metal, an alkaline earth metal, or an ammonium compound of hydroxide, carbonate, bicarbonate, or metasilicate, or any combination thereof;c) calcining the impregnated alumina support in a non-reducing atmosphere for a time and a temperature sufficient to at least partially decompose the palladium salt and the gold salt; andd) reducing the calcined impregnated alumina support comprising partially decomposed palladium and gold salts with a reducing agent for a time and a temperature sufficient to provide a supported catalyst comprising palladium metal and gold metal.2. A process for preparing a supported catalyst according to claim 1 , further comprising after the contacting step claim 1 , the steps of [b1] drying the impregnated alumina support; [b2] washing the impregnated alumina support with water; and [b3] drying the impregnated alumina support following washing.3. A ...

POROUS BODIES WITH ENHANCED PORE ARCHITECTURE

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

PROCESS FOR PREPARING POROUS IRON OXIDE-ZIRCONIA COMPOSITE CATALYST, POROUS IRON OXIDE-ZIRCONIA COMPOSITE CATALYST PREPARED THEREBY, AND METHOD FOR PRODUCING ALCOHOL USING THE CATALYST

The present invention relates to a porous iron oxide-zirconia composite catalyst, a preparation method thereof, and a method for producing alcohol using the same, and the iron oxide-zirconia composite catalyst having a porous structure may produce alcohol at low cost by carrying out an excellent methane reforming reaction even under room temperature and room pressure conditions through an electrochemical reaction. 1. A method for preparing a porous iron oxide-zirconia composite catalyst , the method including:impregnating a polymer template mold with a precursor mixture of iron oxide precursor and a zirconia precursor;drying the polymer template mold impregnated with the precursor mixture; andsintering the dried polymer template mold.2. The method of claim 1 ,wherein the iron oxide precursor is one or more selected from the group consisting of iron (III) nitrate, iron (III) chlorate, and iron (III) sulfate.3. The method of claim 1 ,wherein the zirconia precursor is one or more selected from the group consisting of zirconium oxynitrate, zirconium nitrate, and zirconium sulfate.4. The method of claim 1 ,wherein the iron oxide precursor and the zirconia precursor are mixed at a molar ratio of 8:1 to 2:1.5. The method of claim 1 ,wherein the polymer template mold includes a spherical polymer arranged in a face centered cubic (fcc) structure.6. The method of claim 1 ,wherein the polymer template mold is manufactured by a method including emulsion polymerization of monomers, followed by drying step.7. The method of claim 1 ,wherein the polymer template mold includes one or more polymers selected from the group consisting of poly(methyl methacrylate) [PMMA], poly(butyl methacrylate) [PBMA], poly(methyl methacrylate)(butyl methacrylate), poly(hydroxyethyl methacrylate) [PHEMA], and polystyrene.815-. (canceled) This application is a divisional of U.S. patent application Ser. No. 16/134,424, filed Sep. 18, 2018, which claims priority to Korean Patent Application No. 10-2018- ...

EPOXIDATION PROCESS

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

Supported perovskite-oxide composites for enhanced low temperature thermochemical conversion of co2 to co

Disclosed herein is a catalyst composite containing a perovskite-oxide and an oxide support, methods of preparing a catalyst composite containing a perovskite-oxide and an oxide support, and the use thereof for CO2 conversion by a reverse water gas shift chemical looping (RWGS-CL) process.

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

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

CARBON NITRIDE HETEROGENEOUS CATALYST CONTAINING RHODIUM, METHOD FOR PREPARING THE SAME, AND METHOD FOR PREPARING ACETIC ACID USING THE SAME

A carbon nitride heterogeneous catalyst containing rhodium, a method for preparing the catalyst, and a method for preparing acetic acid using the catalyst is disclosed. The heterogeneous catalyst is characterized in that the rhodium metal is contained in carbon nitride which is a support insoluble in a liquid solvent, such as water or alcohol. Thus, the catalyst can easily be separated from a resulting product even by a simple process such as filtration. Accordingly, the carbon nitride heterogeneous catalyst exhibits excellent long-term stability and activity by being capable of overcoming the disadvantages of the method using a conventional homogeneous catalyst and minimizing the phenomenon of rhodium leaching, compared to the results of the conventional homogeneous catalytic reactions. The catalyst can thus be effectively used for the preparation of acetic acid by a carbonylation reaction between methanol and carbon monoxide. 1. A composite catalyst for an alcohol carbonylation , comprising a first catalyst of carbon nitride support and a second catalyst of rhodium dispersed in the network of the carbon nitride support to reduce the leaching level of the rhodium in the alcohol carbonylation.2. The composite catalyst of claim 1 , wherein the rhodium is contained in an amount of 0.1 wt % to 10 wt % based on the total weight of the carbon nitride.3. The composite catalyst of claim 1 , wherein the composite catalyst has a specific surface area in a range of 0.5 m/g to 100 m/g.4. The composite catalyst of claim 1 , wherein the carbon nitride is at least one kind selected from the group consisting of graphite carbon nitride claim 1 , α-carbon nitride claim 1 , β-carbon nitride claim 1 , cubic carbon nitride claim 1 , and pseudocubic carbon nitride.5. The composite catalyst of claim 1 , wherein the alcohol is methanol or ethanol.6. A method of preparing a composite catalyst comprising carbon nitride support and rhodium dispersed therein claim 1 , comprising heating a ...

ALUMINA-SUPPORTED VANADIUM OXIDE DEHYDROGENATION CATALYST

Fluidizable catalysts for the gas phase oxygen-free oxidative dehydrogenation of alkanes, such as propane, to corresponding olefins, such as propylene. The catalysts comprise 5-20% by weight per total catalyst weight of one or more vanadium oxides (VO), such as VO. The dehydrogenation catalysts are disposed on an alumina support that is modified with calcium oxide to influence characteristics of lattice oxygen at the catalyst surface. Various methods of preparing and characterizing the catalyst as well as methods for the gas phase oxygen free oxidative dehydrogenation of alkanes, such as propane, to corresponding olefins, such as propylene, with improved alkane conversion and olefin product selectivity are also disclosed. 1. An alumina-supported dehydrogenation catalyst , comprising:a support material comprising alumina modified by calcium oxide, wherein a weight ratio of calcium oxide to alumina is from 1:0.2 to 1:1; and{'sub': 2', '5', '2', '3, 'a catalytic material comprising one or more vanadium oxides disposed on the support material, wherein the one or more vanadium oxides is selected from the group consisting of VOand VO;'}wherein the dehydrogenation catalyst comprises 5-20% of the one or more vanadium oxides by weight relative to the total weight of the dehydrogenation catalyst.23-. (canceled)4. The alumina-supported dehydrogenation catalyst of claim 1 , wherein the one or more vanadium oxides form an amorphous phase on the surface of the support material.5. (canceled)6. The alumina-supported dehydrogenation catalyst of claim 1 , which comprises at least 50% of VOby weight relative to the total weight of the one or more vanadium oxides.7. The alumina-supported dehydrogenation catalyst of claim 1 , which has an average particle size in the range of 20-160 μm.820-. (canceled) The present disclosure relates to fluidizable vanadium based VO/CaO-γ-AlOcatalysts and dehydrogenation processes using the catalysts for the oxidative dehydrogenation of alkanes, such as ...

CERAMIC CATALYTIC FILTER, FILTERING SYSTEM INCLUDING THE SAME, AND MANUFACTURING METHOD THEREOF

A ceramic catalyst filter, a filtering system including the same, and a method of manufacturing the same. The ceramic catalyst filter includes: a single body ceramic filter including a first surface for blocking a first material and a second surface for removing the second material passing through the first surface; and a photocatalyst thin film including nanometer-scale grains coated on a surface of the ceramic filter. 1. A ceramic catalyst filter comprising:a single body ceramic filter comprising a first surface for blocking a first material and a second surface for removing a second material passing through the first surface; anda photocatalyst thin film comprising nanometer-scale grains coated on a surface of the ceramic filter.2. The ceramic catalyst filter of claim 1 ,wherein the grains form a worm-like alignment structure.3. The ceramic catalyst filter of claim 1 ,wherein the grains have an average grain size of about 1 nanometer to about 1,000 nanometers.4. The ceramic catalyst filter of claim 1 ,{'sup': '−3', 'wherein the photocatalyst thin film has a specific surface area of about 1 to about 300 square meters per gram, pores having a diameter of about 1 to about 100 nanometers, and a pore volume in a range of about 1×10to about 1 cubic centimeters per gram.'}5. The ceramic catalyst filter of claim 1 ,wherein the photocatalyst thin film comprises a metal oxide photocatalyst.6. The ceramic catalyst filter of claim 5 ,{'sub': 2', '3', '2', '3', '4', '2', '3', '2', '3', '3', '4, 'wherein the metal oxide photocatalyst comprises TiO, WO, FeO, BiVO, ZnO, SiO, BaTiO, FeO, FeO, or a combination thereof.'}7. The ceramic catalyst filter of claim 5 ,wherein the photocatalyst thin film further comprises a cocatalyst for improving photolysis characteristics or pyrolysis characteristics of the metal oxide metal oxide photocatalyst, wherein the cocatalyst comprises:i) a metal compound capable of performing an oxygen generation reaction or an oxygen reduction reaction;ii) ...

COMPOSITE MATERIAL COMPRISING AN ELECTRIDE COMPOUND

A process for preparing a composite material comprising an electride compound and an additive, said process comprising (i) providing a composition comprising the additive and a precursor compound of the electride compound, wherein the precursor compound comprises an oxidic compound of the garnet group, and wherein the additive has a boiling temperature which is higher than the melting temperature of the precursor compound; (ii) heating the composition provided in (i) under plasma forming conditions in a gas atmosphere to a temperature above the Hüttig temperature of the precursor compound and below the boiling temperature of the additive, obtaining the composite material. 120-. (canceled)21. A process for preparing a composite material comprising an electride compound and an additive , said process comprising(i) providing a composition comprising the additive and a precursor compound of the electride compound, wherein the precursor compound comprises an oxidic compound of the garnet group, and wherein the additive has a boiling temperature which is higher than the melting point of the precursor compound;(ii) heating the composition provided in (i) under plasma forming conditions in a gas atmosphere to a temperature above the Hüttig temperature of the precursor compound and below the boiling temperature of the additive, obtaining the composite material.22. The process of claim 21 , wherein according to (ii) claim 21 , heating the composition under plasma forming conditions comprises heating the composition in an electric arc claim 21 , wherein according to (ii) claim 21 , the composition provided in (i) is heated to a temperature above the Tamman temperature of the precursor compound and below the boiling temperature of the additive claim 21 , preferably Wherein according to (ii) claim 21 , the composition provided in (i) is heated to a temperature above the melting temperature of the precursor compound and below the boiling temperature of the additive.23. The ...

HETEROGENEOUS CATALYST PROCESS AND NICKEL CATALYST

The present invention relates to heterogeneous catalysts and methods of making and using the same. In various embodiments, the present invention provides a method of making a hydrogenation catalyst including particulate nickel metal (Ni(0)). The method includes calcining first nickel(II)-containing particles in an atmosphere including oxidizing constituents to generate second nickel(II)-containing particles. The method also includes reducing the second nickel(II)-containing particles in a reducing atmosphere while rotating or turning the second nickel(II)-containing particles at about 275° C. to about 360° C. for a time sufficient to generate the particulate nickel metal (Ni(0)), wherein the particulate nickel metal (Ni(0)) is free flowing. 1. A method of making a heterogeneous catalyst comprising particulate nickel metal (Ni(0)) , the method comprising:calcining first nickel(II)-containing particles in an atmosphere comprising oxidizing constituents to generate second nickel(II)-containing particles; andreducing the second nickel(II)-containing particles in a reducing atmosphere while rotating or turning the second nickel(II)-containing particles at about 275° C. to about 360° C. for a time sufficient to generate the particulate nickel metal (Ni(0)), wherein the particulate nickel metal (Ni(0)) is free flowing.2. The method of claim 1 , wherein neither water nor steam are added to the reducing atmosphere.3. The method of wherein the second nickel(II)-containing particles comprise basic nickel carbonate claim 1 , nickel oxide claim 1 , nickel carbonate claim 1 , nickel bicarbonate claim 1 , nickel oxalate claim 1 , nickel formate claim 1 , nickel squarate claim 1 , nickel hydroxide claim 1 , nickel nitrate claim 1 , nickel cyanate claim 1 , nickel sulfate and combinations thereof.4. The method of claim 1 , wherein calcining comprises heating the first nickel(II)-containing particles in an atmosphere comprising the oxidizing constituents at a temperature of about 350 ...

ETHYLENE EPOXIDATION CATALYSTS, ASSOCIATED METHODS OF MANUFACTURE, AND ASSOCIATED METHODS FOR THE PRODUCTION OF ETHYLENE OXIDE

An ethylene epoxidation catalyst is disclosed that comprises a fluoride-mineralized carrier having silver and a rhenium promoter deposited thereon, wherein the fluoride-mineralized carrier has: a total fluorine (TF) content less than 5000 ppm as measured by XRF, a water extractable fluorine (WEF) content greater than 45 ppm as measured by microwave extraction and ion specific electrode, and wherein the ratio of TF:WEF is between 10 and 110. Associated methods of manufacturing such catalysts and epoxidation methods using such catalysts are similarly provided. 1. An ethylene epoxidation catalyst comprising a fluoride-mineralized carrier having silver and a rhenium promoter deposited thereon , wherein the fluoride-mineralized carrier has:a total fluorine (TF) content less than 5000 ppm as measured by XRF,a water extractable fluorine (WEF) content greater than 45 ppm as measured by microwave extraction and ion specific electrode, andwherein the ratio of TF:WEF is between 10 and 110.2. The ethylene epoxidation catalyst of wherein the ratio of TF:WEF is greater than 15.3. The ethylene epoxidation catalyst of wherein the ratio of TF:WEF is less than 90.4. The ethylene epoxidation catalyst of wherein the ratio of TF:WEF is less than 70.5. The ethylene epoxidation catalyst of wherein the WEF is greater than 50 ppm.6. The ethylene epoxidation catalyst of wherein the WEF is greater than 100 ppm.7. The ethylene epoxidation catalyst of wherein the WEF is less than 300 ppm.8. The ethylene epoxidation catalyst of wherein the WEF is less than 200 ppm.9. The ethylene epoxidation catalyst of wherein the WEF is less than 180 ppm.10. The ethylene epoxidation catalyst of wherein the TF is greater than 2000 ppm.11. The ethylene epoxidation catalyst of wherein the TF is greater than 2500 ppm.12. The ethylene epoxidation catalyst of wherein the TF is less than 4500 ppm.13. The ethylene epoxidation catalyst of wherein the fluoride-mineralized carrier has a water absorption of at least 50 ...

SHELL IMPREGNATED CATALYST AND PROCESS FOR PRODUCING A SHELL IMPREGNATED CATALYST BODY

The present application relates to a process for producing a catalyst,said process comprising the steps of: providing a carrier and following modifying said carrier by a first impregnation with at least one alkaline earth metal in a first metal precursor solution. The first metal precursor is decomposed to form at least one metal oxide or metal hydroxide thereby obtaining a modified carrier and a second impregnation is carried out by incipient wetness by a second precursor solution comprising at least one metal Me in a second solution. Finally the second precursor is decomposed thereby obtaining a catalyst body having an enrichment of the at least one metal Me in the outer shell of the catalyst body, said at least one metal being present in a concentration having either as an egg-shell profile or a hammock profile. 1. A process for producing a catalyst , said process comprising the steps of:providing a carriermodifying said carrier by a first impregnation with at least one alkaline earth metal in a first metal precursor solutiondecomposing the first metal precursor to form at least one metal oxide or metal hydroxide thereby obtaining a modified carriercarrying out a second impregnation by incipient wetness by a second precursor solution comprising at least one metal Me in a second solutiondecomposing the second precursor thereby obtaining a catalyst body having an enrichment of the at least one metal Me in the outer shell of the catalyst body, said at least one metal being present in a concentration having either an egg-shell profile and/or a hammock profile.2. A process according to wherein the carrier is alumina spinel and/or calcium aluminate.3. Process according to claim 1 , wherein carrier has a pore volume 200-400 ml/kg claim 1 , and/or BET surface area 2-50 m/g.4. Process according to claim 1 , comprising repeating the second impregnation one or more times.5. A process according to claim 1 , wherein the first precursor solution is a nitrate claim 1 , ...

Compositions of chromium oxyfluoride or fluoride catalysts, their preparation and their use in gas-phase processes

The present invention relates to a process for modifying the fluorine distribution in a hydrocarbon compound in the presence of a catalyst, characterized by the use, as catalyst, of a solid composition comprising at least one component containing chromium oxyfluoride or fluoride of empirical formula Cr x M (1-x) O r F s , where 2r+s is greater than or equal to 2.9 and less than 6, M is a metal chosen from columns 2 to 12 of the Periodic Table of the Elements, x has a value from 0.9 to 1, s is greater than 0 and less than or equal to 6 and r is greater than or equal to 0 and less than 3, the said solid composition having a crystallinity of less than 20% by weight. The present invention also relates to the solid composition per se.

NANO-NICKEL CATALYST AND HYDROGENATION DEVICE OF CARBON OXIDES

A nano-nickel catalyst and a hydrogenation device of carbon oxides are provided. The hydrogenation device is configured to reduce the carbon oxides to form low carbon hydrocarbons. The nano-nickel catalyst has a metallic nickel body and a plurality of microstructures connecting with at least one surface of the metallic nickel body. The microstructures are sharp, and have a length-diameter ratio ranging from 2 to 5. 1. A nano-nickel catalyst , comprising:a metallic nickel body; anda plurality of microstructures connected to the metallic nickel body on at least one surface of the metallic nickel body;wherein the microstructures are sharp, and have a length-diameter ratio ranging from 2 to 5.2. The nano-nickel catalyst according to claim 1 , wherein the microstructures contain metallic nickel.3. The nano-nickel catalyst according to claim 2 , wherein the microstructures are made of metallic nickel.4. The nano-nickel catalyst according to claim 1 , wherein the metallic nickel body is spherical.5. The nano-nickel catalyst according to claim 1 , wherein the metallic nickel body is porous.6. The nano-nickel catalyst according to claim 1 , wherein the metallic nickel body is solid.7. The nano-nickel catalyst according to claim 1 , wherein the metallic nickel body is hollow.8. The nano-nickel catalyst according to claim 5 , wherein the metallic nickel body is porous claim 5 , and has an adsorption pore volume ranging from 0.0024 cm/g to 0.0062 cm/g.9. The nano-nickel catalyst according to claim 1 , wherein the nano-nickel catalyst has a specific surface area ranging from 1.5 m/g to 2.0 m/g.10. The nano-nickel catalyst according to claim 1 , wherein the nano-nickel catalyst has an ability to reduce carbon dioxide into low-carbon hydrocarbons.11. The nano-nickel catalyst according to claim 10 , wherein the low-carbon hydrocarbons are selected from a group consisting of methane claim 10 , ethane claim 10 , propane claim 10 , and a combination thereof.12. A hydrogenation device ...

CATALYST SUPPORTS MADE FROM SILICON CARBIDE COVERED WITH TIO2 FOR FISCHER-TROPSCH SYNTHESIS

Catalysts supports and catalysts capable of being used in heterogeneous catalysis. The catalyst support belongs to the porous supports based on silicon carbide (SiC), in particular, based on β-SiC, modified by a surface deposit of TiO. 125-. (canceled)26. Use , for a Fischer-Tropsch reaction , of an SiC-based catalyst support at least partially covered with TiOcapable of being obtained by a preparation method comprising:providing a highly porous β-SiC support;{'sub': '2', 'preparing a solution of at least one TiOprecursor;'}impregnating said highly porous β-SiC support by said solution;drying said impregnated highly porous β-SiC support; and{'sub': 2', '2, 'calcining said impregnated highly porous β-SiC support in order to transform said TiOprecursor into TiO.'}27. The use of claim 26 , wherein said highly porous β-SiC support is in the form of extrudates claim 26 , pellets claim 26 , beads claim 26 , microbeads or cellular foam.28. The use of claim 26 , wherein a specific surface of said highly porous β-SiC support is at least 20 m/g.29. The use of claim 28 , wherein a microporous contribution to the specific surface of said highly porous β-SiC support is less than 5 m/g.30. The use of claim 26 , wherein said calcination is performed at a temperature of between 500° C. and 900° C.31. The use of claim 30 , wherein claim 30 , in said calcination claim 30 , a temperature increase is produced with a gradient of between 1.5° C./min and 2.5° C./min.32. The use of claim 26 , wherein claim 26 , in said catalyst support claim 26 , a TiO/SiC mass ratio is between 8% and 13%.337. The use of claim claim 26 , wherein claim 26 , in said catalyst support claim 26 , a TiOcontent is less than 0.009 g per mof a specific surface of the highly porous β-SiC support.34. A method for catalytic conversion of CO and hydrogen into hydrocarbons claim 26 , and which involves a catalyst obtained by a deposition of an active phase on an SiC-based catalyst support at least partially covered with ...

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

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

METHOD FOR PRODUCING CATALYST MONOLITHS FOR THE REFORMING OF HYDROCARBONS

A method for producing a three-dimensional porous catalyst monolith of stacked catalyst fibers, comprising the following steps: a) Preparing a suspension paste in a liquid diluent of a reforming catalyst, and which suspension can furthermore comprise a binder material, all particles in the suspension having an average particle size in the range of from 0.5 to 500 μm, b) extruding the paste of step a) through one or more nozzles to form fibers, and depositing the extruded fibers to form a three-dimensional porous catalyst monolith precursor, c) drying the porous catalyst monolith precursor to remove the liquid diluent, d) calcining the porous catalyst monolith precursor to form the porous catalyst monolith. 116.-. (canceled)17. A method for producing a three-dimensional porous catalyst monolith of stacked catalyst fibers , comprising the following steps:a) Preparing a suspension paste in a liquid diluent of particles of a catalyst A, which comprises at least nickel-magnesium mixed oxide and magnesium spinel and optionally aluminum oxide hydroxide, wherein the nickel-magnesium mixed oxide has an average crystallite size of ≤100 nm, the magnesium spinel phase has an average crystallite size of ≤100 nm, the proportion of nickel in the catalyst is in the region of 30 mol %, the proportion of magnesium is in the range 8-38 mol %, and the proportion of aluminum is in the range 50-70 mol % and the intensity of the diffraction reflection of the catalyst at 43.09°2θ is less than or equal to the intensity of the diffraction reflection at 44.82°2θ, with the intensity of the diffraction reflection at 43.08°2θ or of a hexaaluminate-comprising catalyst B, which comprises cobalt and at least one further metal from the group consisting of Ba, Sr, La, or of precursors of catalyst A or B, and which suspension can furthermore comprise 1 to 15 wt %, based on the suspension paste, of a binder material, selected from the group of organic and inorganic binders and mixtures thereof, all ...

NaY molecular sieve with an aluminum-rich surface and a process of preparing same

A NaY molecular sieve with an aluminum-rich surface is prepared using a process that includes the steps of: a. mixing a directing agent and a first silicon source to obtain a first mixture, wherein the directing agent has a molar composition of NaO: AlO: SiO: HO=(6-25): 1: (6-25): (200-400); b. mixing the first mixture obtained in the step a with a second silicon source, an aluminum source and water to obtain a second mixture; c. carrying out hydrothermal crystallization on the second mixture obtained in the step b, and collecting a solid product. Calculated as SiO, the weight ratio of the first silicon source to the second silicon source is 1: (0.01-12). The NaY molecular sieve has larger aluminum distribution gradient from the surface to the center of the particle than the conventional molecular sieve. 1. A NaY molecular sieve with an aluminum-enriched surface , characterized in that the Al distribution index , D , of the molecular sieve satisfies: 1.01≤D≤preferably 1.1≤D≤6 , more preferably 1.2 or 1.3≤D≤4 , {'br': None, 'D=Al (S)/Al (C),'}, 'wherein'}Al (S) denotes the aluminum content on surface and in the region 2 to 6 nm below the surface of the molecular sieve, as measured by the XPS method, andAl (C) denotes the aluminum content of the entire molecular sieve, as measured by the XRF method.2. The NaY molecular sieve according to claim 1 , characterized in that the molecular sieve with an aluminum-rich surface has a molar ratio of SiO/AlOon surface of 1 to 10 claim 1 , preferably 2 to 8 claim 1 , and more preferably 2.5 to 5 claim 1 , and a molar ratio of SiO/AlOin bulk phase of 2 to 20 claim 1 , preferably 4 to 15 claim 1 , and more preferably 6 to 10.3. The NaY molecular sieve according to claim 1 , characterized in that the NaY molecular sieve with an aluminum-rich surface has an Al content claim 1 , calculated as AlO claim 1 , of 18-26 wt % claim 1 , preferably 21-25 wt %.4. The NaY molecular sieve according to claim 1 , characterized in that the NaY ...

PROPYLENE DIRECT OXIDATION REACTION CATALYST, METHOD FOR PREPARING SAME, AND METHOD FOR PREPARING PROPYLENE OXIDE THROUGH PROPYLENE DIRECT OXIDATION REACTION USING SAME

Disclosed is a propylene direct oxidation reaction catalyst capable of preparing a propylene oxide from propylene and oxygen at a higher yield than catalysts prepared by conventional methods, by applying a specific transition metal oxide promoter in preparation of a catalyst containing silver, a transition metal oxide promoter and a carrier through a slurry process. The present invention provides a propylene direct oxidation reaction catalyst, which is a supported silver catalyst used for preparing a propylene oxide from the propylene direct oxidation reaction, the catalyst including a molybdenum oxide and a tungsten oxide as a catalyst promoter. 1. A propylene direct oxidation reaction catalyst , which is a supported silver catalyst used for preparing a propylene oxide from a propylene direct oxidation reaction , the catalyst comprising , as a catalyst promoter , a molybdenum oxide (MoO) and a tungsten oxide (WO).2. The propylene direct oxidation reaction catalyst of claim 1 , wherein the silver is included in an amount of 5-30% by weight with respect to the entire catalyst.3. The propylene direct oxidation reaction catalyst of claim 1 , wherein the promoter is included in an amount of 1-20% by weight with respect to the entire catalyst.4. The propylene direct oxidation reaction catalyst of claim 1 , wherein the molybdenum oxide to the tungsten oxide is included claim 1 , by weight percentage claim 1 , at a ratio of 1:99 to 99:1.5. The propylene direct oxidation reaction catalyst of claim 1 , wherein a carrier used for the support is a zirconium oxide.6. The propylene direct oxidation reaction catalyst of claim 5 , wherein the zirconium oxide is prepared according to a method comprising the steps of:(i) dissolving a zirconium oxide precursor in a solvent to prepare a zirconium oxide precursor solution;(ii) adding a basic aqueous solution to the zirconium oxide precursor solution;(iii) stirring the solution prepared in the step (ii) and then filtering to obtain a ...

PROCESS FOR PREPARING AN EPOXIDATION CATALYST

A process for preparing a silver-containing catalyst for the selective oxidation of ethylene to ethylene oxide including the steps of: (a) providing a multimodal support, (b) preparing an impregnation solution comprising a silver component, (c) impregnating, at least once, the multimodal support of step (a) with the silver-containing impregnation solution of step (b) to form an impregnated support; (d) subjecting the impregnated multimodal support from step (c) to a removal means, such as a centrifuge, at least once, for a time sufficient to remove impregnated silver impregnation solution from the multimodal support and to control the amount of silver in the pores of the multimodal support by selectively removing impregnated silver impregnation solution from a set of larger pores in the multimodal support; (e) roasting, at least once, the multimodal support after the step (d); (f) optionally, repeating the impregnation step (c), (g) optionally, repeating the centrifugation step (d), and (h) optionally, repeating the calcination step (e). 1. A process for preparing a silver-containing catalyst for the epoxidation of olefins comprising the steps of:(a) providing a porous multimodal support having at least a first set of support pores of a first size range and at least a second set of support pores of a second size range wherein the second size range of the second set of support pores is smaller than the first size range of the first set of support pores;(b) providing a first silver-containing impregnation solution for impregnating the first silver-containing impregnation solution into the at least first set of support pores and the at least second set of support pores of the porous multimodal support;(c) impregnating, one or more times, the porous multimodal support with the first silver-containing impregnation solution from step (b) to provide the porous multimodal support with a first amount of silver-containing impregnation solution; and(d) selectively removing at ...

PROMOTER METAL CONTAINING PEROVSKITE-TYPE COMPOUND FOR GASOLINE EXHAUST GAS APPLICATIONS

A three-way catalyst composition, and its use in an exhaust system for internal combustion engines, is disclosed. The composition can comprise a compound of formula (I): AA′BB′Oand a promoter metal component, wherein A is an ion of a metal of group 2 or 3 of the periodic table of elements; wherein A′ is an ion of a metal of group 1, 2, or 3 of the periodic table of elements; wherein B and B′ are ions of metal of groups 4, 6, 7, 8, 9, 10, 11, or 13 of the periodic table of elements; wherein x is from 0.7 to 1; wherein y is from 0 to 0.5; and wherein z is from 0 to 0.5. 1. A composition comprising a perovskite type compound of formula (I): AA′BB′Oand a promoter metal component , wherein A is an ion of a metal of group 2 or 3 of the periodic table of elements; wherein A′ is an ion of a metal of group 1 , 2 , or 3 of the periodic table of elements; wherein B and B′ are ions of metal of groups 4 , 6 , 7 , 8 , 9 , 10 , 11 , or 13 of the periodic table of elements; wherein x is from 0.7 to 1; wherein y is from 0 to 0.5; and wherein z is from 0 to 0.5.2. The composition of claim 1 , wherein A is Y claim 1 , La claim 1 , Nd claim 1 , Ce claim 1 , or Gd.3. The composition of claim 2 , wherein A is La or Y.4. The composition of claim 1 , wherein A′ is Sr claim 1 , Ca claim 1 , Y claim 1 , or Ce.5. The composition of claim 1 , wherein B is Mn claim 1 , Co claim 1 , Fe claim 1 , or Ni.6. The composition of claim 5 , wherein B is Mn or Fe.7. The composition of claim 6 , wherein B is Fe.8. The composition of claim 1 , wherein B′ is Mn claim 1 , Fe claim 1 , Ni claim 1 , Co claim 1 , or Cu.9. The composition of claim 8 , wherein B′ is Cu.10. The composition of claim 1 , wherein x is from 0.8 to 1.11. The composition of claim 1 , wherein y is from 0 to 0.4.12. (canceled)13. The composition of claim 1 , wherein z is from 0 to 0.4.14. (canceled)15. The composition of claim 1 , wherein the specific surface area of the compound of formula (I) is at least 8 m/g.16. The composition of ...

METHOD OF PREPARING A CATALYTIC STRUCTURE

A method of preparing a catalytic structure the method including the steps of: providing a solution of a precursor compound in a solvent at ambient conditions; providing a suspension of a support material having a specific surface area of at least 1 m2/g in a solvent at ambient conditions; mixing the solution of the precursor compound and the suspension of the support material; providing a reactive solvent in a supercritical or subcritical state; admixing the mixture of the solution of the precursor compound and the suspension of the support material in the supercritical or subcritical reactive solvent to form a reaction solution; injecting the reaction solution into a reactor tube via an inlet; allowing a reaction of the precursor compound in the supercritical or subcritical reactive solvent in the reactor tube to form the catalyst nanoparticles on the support material to provide the catalytic structure. 131-. (canceled)32. A method of preparing a catalytic structure having catalyst nanoparticles , the method comprising the steps of;providing a solution of a precursor compound in a solvent at ambient conditions;{'sup': '2', 'providing a suspension of a support material having a specific surface area of at least 1 m/g in a solvent at ambient conditions;'}optionally sonicating the suspension of the support material;mixing the solution of the precursor compound and the suspension of the support material;providing a reactive solvent in a supercritical or subcritical state;admixing the mixture of the solution of the precursor compound and the suspension of the support material in the supercritical or subcritical reactive solvent to form a reaction solution;injecting the reaction solution into a reactor tube via an inlet;allowing a reaction of the precursor compound in the supercritical or subcritical reactive solvent in the reactor tube to form the catalyst nanoparticles on the support material to provide the catalytic structure; andwithdrawing the catalytic structure ...

RETAINING MATERIAL FOR POLLUTION CONTROL ELEMENT, METHOD FOR MANUFACTURING THE SAME, AND POLLUTION CONTROL DEVICE

A retaining material that can sufficiently maintain the function of retaining a pollution control element in a pollution control device at high temperature. In one aspect, the retaining material has a mat shape and contains inorganic fiber material, with the retaining material containing: a surface layer containing inorganic colloid particles; and an internal region positioned further to the inside than the surface layer, impregnated with inorganic colloid particles and organic binder; wherein the surface layer contains inorganic colloid particles at a higher concentration than the internal region; and the amount of inorganic colloid particles in the internal region is 1 mass % to 10 mass % based on the total mass of the retaining material. 1. A method for manufacturing a retaining material , comprising:a step of impregnating a first liquid containing inorganic colloid particles and an organic binder into a sheet including an inorganic fiber material so that inorganic colloid particles are essentially uniformly dispersed in the thickness direction of the sheet and organic binder is essentially uniformly dispersed in the thickness direction of the sheet;a step of drying the sheet impregnated with the first liquid; anda step of forming a surface layer by coating a surface of the sheet with a second liquid containing inorganic colloid particles.2. The method according to claim 1 , wherein the second liquid is coated respectively onto opposite surfaces of the sheet.3. The method according to claim 1 , wherein the composition of the first liquid is adjusted such that the amount of inorganic colloid particles in an internal region of the sheet positioned further to the inside than the surface layer is 1 mass % to 10 mass % based on the total mass of the internal region.4. The method according to claim 1 , wherein the composition of the second liquid and the amount of coating of the second liquid are adjusted such that the amount of inorganic colloid particles per unit ...

PROCESS FOR CONVERSION OF SULFUR TRIOXIDE AND HYDROGEN PRODUCTION

The present disclosure relates to a process for decomposition of sulfuric acid, particularly a process for catalytically decomposing sulfuric acid, to obtain sulfur dioxide therefrom. In the present process, catalysts play a major role for improving the dissociation efficiency by lowering the activation energy barrier for the reaction. 1. A process for conversion of sulphur trioxide to sulphur dioxide and oxygen comprising , the process comprising;placing a catalyst composition in a reactor, wherein the catalyst composition comprises an active material selected from the group consisting of transitional metal oxide, mixed transitional metal oxide, and combinations thereof; and a support material selected from the group consisting of silica, titania, zirconia, carbides, and combinations thereof, wherein the active material to the support material weight ratio is in the range of 0.1 to 25 wt %;passing a flow of sulphur trioxide in the presence of an optionally used carrier gas over the catalyst composition at a temperature of 700° C.-900° C.; andrecovering stream comprising of sulphur trioxide, sulphur dioxide, oxygen, water, and the optionally used carrier gas.2. The process as claimed in claim 1 , wherein the transitional metal is selected from the group consisting of Cu claim 1 , Cr claim 1 , and Fe.3. The process as claimed in claim 1 , wherein the active material is transitional metal oxide selected from the group consisting oxides of Cu claim 1 , Cr claim 1 , and Fe.4. The process as claimed in claim 1 , wherein the active material is mixed transitional metal oxide selected from the group consisting of binary oxide claim 1 , a ternary oxide claim 1 , and a spinel.5. The process as claimed in claim 1 , wherein the active material is an oxide of Cu.6. The process as claimed in claim 1 , wherein the active material is an oxide of Cr.7. The process as claimed in claim 1 , wherein the active material is an oxide of Fe.8. The process as claimed in claim 1 , wherein the ...

INTERESTERIFICATION CATALYST AND PROCESS

A process for the production of an ester product from a mixture of at least two different ester compounds includes the steps of mixing together at least two different starting ester compounds to form a first ester mixture; and contacting the first ester mixture with a catalyst including from 30-60% of calcium oxide and at least one second metal oxide at a temperature of at least 180° C., for a duration of at least one hour, with mixing, to form a second ester mixture having a melting point which is lower than the melting point of the first ester mixture. 1. A process for the production of an ester product from a mixture of at least two different ester compounds comprises the steps of:a) mixing together at least two different starting ester compounds to form a first ester mixture; andb) contacting said first ester mixture with a catalyst comprising from 30-60% of calcium oxide and at least one second metal oxide to form a second ester mixture having a melting point which is lower than the melting point of said first ester mixture.2. A process as claimed in claim 1 , wherein at least one of the starting esters is a triglyceride.3. A process as claimed in claim 1 , wherein at least one of the starting ester compounds comprises an ester of a carboxylic acid containing from 12 to 24 carbon atoms.4. A process as claimed in claim 1 , wherein the catalyst is pre-dispersed in at least one of said starting ester compounds.5. A process as claimed in claim 1 , wherein the second metal oxide is selected from the group consisting of an oxide of a Group 2A metal other than calcium claim 1 , an oxide of a transition metal claim 1 , lanthana claim 1 , silica claim 1 , alumina and a metal aluminate.6. A process as claimed in claim 5 , wherein the second metal oxide comprises magnesium oxide.7. A process as claimed in claim 1 , wherein the catalyst further comprises from 1-5% of an alkali metal.8. A process as claimed in claim 1 , wherein the catalyst has a surface area less than 20 m ...

Selective Hydrogenation Catalyst and Methods of Making and Using Same

A composition comprising an extruded inorganic support comprising an oxide of a metal or metalloid, and at least one catalytically active metal, wherein the extruded inorganic support has pores, a total pore volume, and a pore size distribution, wherein the pore size distribution displays at least two peaks of pore diameters, each peak having a maximum, wherein a first peak has a first maximum of pore diameters of equal to or greater than about 120 nm and a second peak has a second maximum of pore diameters of less than about 120 nm, and wherein greater than or equal to about 5% of a total pore volume of the extruded inorganic support is contained within the first peak of pore diameters.

Exhaust-Gas-Purification Catalyst Carrier

Provided is an exhaust-gas-purification catalyst carrier that contains a ceria-zirconia complex oxide having a pyrochlore phase and a novel exhaust-gas-purification catalyst carrier that exhibit excellent OSC performance at any temperature region of a low temperature (around 400° C.) and a high temperature (around 800° C.). Proposed is the exhaust-gas-purification catalyst carrier containing a ceria-zirconia complex oxide which has a pyrochlore phase and is 7.0 m/g or more in specific surface area and in the range of 100 Å to 700 Å in crystallite size. 1. An exhaust-gas-purification catalyst carrier comprising a ceria-zirconia complex oxide which has a pyrochlore phase and is 7.0 m/g or more in specific surface area and in the range of 100 Å to 700 Å in crystallite size.2. The exhaust-gas-purification catalyst carrier according to claim 1 , wherein a peak exists in the range of a pore size of 100 nm or smaller in a log differential pore volume distribution measured by a mercury intrusion porosimeter.3. The exhaust-gas-purification catalyst carrier according to claim 1 , wherein a value of crystallite size (Å)×specific surface area (m/g) is in the range of 800 to 3000 (Å·m/g).4. The exhaust-gas-purification catalyst carrier according to claim 1 , wherein a peak intensity ratio (Ip/Im) of a peak Ip indicating a pyrochlore structure existing in the range of 2θ=13.7 to 15.3° to a main peak Im existing in the range of 2θ=28.8 to 29.8° is 0.03 or more in a diffraction pattern of XRD (X-ray diffraction).5. An exhaust-gas-purification catalyst comprising a structure formed by supporting at least Pd as a precious metal on the exhaust-gas-purification catalyst carrier according to .6. The exhaust-gas-purification catalyst carrier according to claim 2 , wherein a value of crystallite size (Å)×specific surface area (m/g) is in the range of 800 to 3000 (Å·m/g).7. The exhaust-gas-purification catalyst carrier according to claim 2 , wherein a peak intensity ratio (Ip/Im) of a peak ...