КАТАЛИЗАТОР ГИДРОЛИЗА С ВЫСОКИМ СОДЕРЖАНИЕМ МЕТАЛЛОВ ДЛЯ КАТАЛИТИЧЕСКОГО ВОССТАНОВЛЕНИЯ СЕРЫ В ГАЗОВОМ ПОТОКЕ

Изобретение относится к составу катализатора, пригодному для каталитического восстановления соединений серы в газовом потоке. Состав катализатора содержит сформированный агломерат совместно перемешанной смеси, содержащий псевдобемит, соединение кобальта и соединение молибдена, причем указанный сформированный агломерат обжигают для получения указанного состава катализатора, содержащего гамма-оксид алюминия, от 7,75 до 15 мас.% молибдена и от 2,85 до 6 мас.% кобальта, где каждый мас.% рассчитан от общей массы указанного состава катализатора и металла в качестве оксида независимо от его фактической формы. Указанный состав катализатора имеет бимодальную поровую структуру, так что менее 6% от общего объема пор указанного состава катализатора приходится на поры диаметром более 10000 Å, и где указанная бимодальная поровая структура указанного состава катализатора дополнительно характеризуется тем, что более чем 15% и менее чем 60% от общего объема пор указанного состава катализатора приходится ...

ПОЛУЧЕНИЕ КАТАЛИЗАТОРА НА ОСНОВЕ ZSM-5; ИСПОЛЬЗОВАНИЕ В СПОСОБЕ ДЕАЛКИЛИРОВАНИЯ ЭТИЛБЕНЗОЛА

Изобретение относится к способу получения каталитической композиции и к способу конверсии ароматических углеводородов, содержащих исходное сырье, с использованием каталитической композиции, полученной таким способом. Способ получения каталитической композиции включает стадии: (а) обработки цеолита ZSM-5 щелочным раствором, содержащим гидроксид металла и имеющим рН по меньшей мере 8, с получением обработанного щелочным раствором цеолита, с последующим промыванием водой и сушкой, а затем подвергания обработанного щелочным раствором цеолита ионному обмену путем обработки цеолита раствором, содержащим соль аммония, для получения обработанного цеолита, (b) экструдирования смеси обработанного цеолита и связующего, где связующее представляет собой огнеупорный оксид, выбранный из группы, состоящей из диоксида кремния, диоксида циркония, диоксида титана и их смесей, и приведение в контакт цеолита с раствором, содержащим фторсодержащее соединение, причем раствор, содержащий фторсодержащее соединение ...

КАТАЛИЗАТОР ДЛЯ КАТАЛИТИЧЕСКОГО КРЕКИНГА, ЕГО ПОЛУЧЕНИЕ И ИСПОЛЬЗОВАНИЕ

Настоящее изобретение относится к катализатору для каталитического крекинга его получению и использованию. Описан катализатор для каталитического крекинга углеводородных нефтепродуктов, включающий подложку, включающую оксид алюминия и молекулярное сито, имеющий следующее распределение пор: 5-70% пор составляют поры размером <2 нм, 5-70% пор - поры размером 2-4 нм, 0-10% пор - поры размером 4-6 нм, 20-80% пор - поры размером 6-20 нм и 0-40% пор - поры размером 20-100 нм, исходя из объема пор размером не более 100 нм. Описан способ получения катализатора, в котором выполняют следующие стадии: смешивают подложку, включающую оксид алюминия и/или его прекурсоры, с молекулярным ситом, суспендируют и сушат смесь с помощью распылительной сушки, при этом на стадии смешивания вводят расширитель пор, при этом расширитель пор может быть выбран из группы, включающей борную кислоту и соли щелочных металлов, при этом весовое соотношение расширителя пор к подложке составляет 0,1:100-15:100 по весу подложки ...

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 И СПОСОБ ПОЛУЧЕНИЯ УГЛЕВОДОРОДОВ И ИХ КИСЛОРОДСОДЕРЖАЩИХ ПРОИЗВОДНЫХ ИЗ СИНТЕЗ-ГАЗА

Изобретение относится к катализаторам и способам получения углеводородов и их кислородсодержащих производных из смеси СО и водорода (синтез-газа). Предложен катализатор получения углеводородов и/или их кислородсодержащих производных из синтез-газа, содержащий не менее 0,4 г/см3 совокупности фаз, представляющей собой фазу каталитически активного металла, закрепленную на фазе подложки оксидной природы, оказывающей активное влияние на дисперсность фазы активного металла или другие ее физико-химические свойства, при этом тело катализатора имеет проницаемость не менее 5•10-15 м2. Предложен способ получения углеводородов и/или их кислородсодержащих производных, включающий пропускание синтез-газа через одно или несколько тел концентрированного проницаемого катализатора. При этом предпочтительно, чтобы один из линейных размеров тела катализатора был сопоставим с наименьшим линейным размером реактора. Технический результат: катализатор позволяет проводить синтез углеводородов и/или их кислородсодержащих ...

САМОАКТИВИРУЮЩИЙСЯ КАТАЛИЗАТОР ГИДРОПРОЦЕССИНГА И СПОСОБ ОБРАБОТКИ ТЯЖЕЛОГО УГЛЕВОДОРОДНОГО СЫРЬЯ

... 1. Самоактивирующийся катализатор гидропроцессинга для обработки тяжелого углеводородного сырья, где указанный катализатор содержит: прокаленную частицу, включающую в себя совместно измельченную смесь, полученную при совместном измельчении порошкообразного неорганического оксида, порошкообразного триоксида молибдена и соединения никеля, с последующим формованием данной совместно измельченной смеси в частицу, которую прокаливают, получая, в результате, прокаленную частицу, где данная прокаленная частица содержит молибден, находящийся в количестве от 1 до 10 массовых процентов, в виде металла и из расчета на общую массу указанной прокаленной частицы, и никель, находящийся в таком количестве, чтобы массовое соотношение указанного никеля к указанному молибдену составляло менее 0,4, и при этом указанная прокаленная частица имеет такое распределение пор по размерам, что менее 70% от общего объема пор указанной прокаленной частицы приходится на поры указанной прокаленной частицы с диаметром от ...

КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ И СПОСОБ ТРАНСАЛКИЛИРОВАНИЯ АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ

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

УЛУЧШЕННЫЙ КАТАЛИЗАТОР ИЗ ДРАГОЦЕННОГО МЕТАЛЛА ДЛЯ ДЕБЕНЗИЛИРОВАНИЯ

... 1. Каталитический композит, содержащий углеродный носитель, содержащий карбонизующийся материал, где углеродный носитель имеет общую площадь поверхности пор около 800 м2/г или более и около 2000 м2/г или менее, и около 20% или менее общей площади поверхности пор является площадью поверхности микропор; катализатор из драгоценного металла. 2. Каталитический композит по п.1, в котором углеродный носитель имеет площадь поверхности микропор около 200 м2/г или менее, и каталитический композит содержит от около 70 до около 99,9 мас.% углеродного носителя и от около 0,1 до около 30 мас.% катализатора из драгоценного металла. 3. Каталитический композит по п.1, в котором углеродный носитель содержит около 0,75 мас.% или менее фосфора, и катализатор из драгоценного металла содержит по меньшей мере один компонент, выбранный из группы, состоящей из палладия, гидроксида палладия, палладия и рения, палладия и родия, палладия и вольфрама, палладия и никеля, палладия и олова, палладия и меди, палладия и ...

СПОСОБЫ ПРОИЗВОДСТВА СЫРОГО ПРОДУКТА И ЕГО КОМПОЗИЦИЙ

... 1. Способ получения сырого продукта, включающий ! контактирование углеводородного сырья с одним или более катализаторами, в результате чего образуется суммарный продукт, который включает сырой продукт, представляющий собой смесь, являющуюся жидкой при 25°С и давлении 0,101 МПа, при этом углеводородное сырье содержит молибден в количестве, по меньшей мере, 0,1 вес.ч./млн и Ni/V/Fe в количестве 10 вес.ч./млн, по меньшей мере, один из катализаторов содержит один или более металлов груаа 6-10 периодической таблицы и/или одно или более соединений одного или более металлов групп 6-10 периодической таблицы, и катализатор, содержащий металлы групп 6-10 периодической таблицы, характеризуется распределением размера пор со средним диаметром пор до 150 Е, и ! контролирование условий контактирования при температуре, по меньшей мере, 300°С, парциальном давлении водорода до 7 МПа и часовой объемной скорости жидкости (ЧОСЖ), по меньшей мере, 0,1 ч-1, в результате чего получают сырой продукт, который содержит ...

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 ...

САМОАКТИВИРУЮЩИЙСЯ КАТАЛИЗАТОР ГИДРООБРАБОТКИ, ОБЛАДАЮЩИЙ ПОВЫШЕННОЙ АКТИВНОСТЬЮ И СВОЙСТВАМИ САМОАКТИВАЦИИ, И ЕГО ИСПОЛЬЗОВАНИЕ ДЛЯ ОБРАБОТКИ ОСТАТОЧНОГО СЫРЬЯ

МЕЗОПОРИСТЫЙ И МАКРОПОРИСТЫЙ КАТАЛИЗАТОР НА ОСНОВЕ НИКЕЛЯ, ПОЛУЧЕННЫЙ СОВМЕСТНЫМ ПЛАСТИЦИРОВАНИЕМ И ИМЕЮЩИЙ МЕДИАННЫЙ ДИАМЕТР МАКРОПОР, ПРЕВЫШАЮЩИЙ 300 НМ, И ЕГО ПРИМЕНЕНИЕ ПРИ ГИДРИРОВАНИИ УГЛЕВОДОРОДОВ

КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ ДЛЯ АЛКИЛИРОВАНИЯ АРОМАТИЧЕСКИХ СОЕДИНЕНИЙ, СПОСОБЫ ИХ АЛКИЛИРОВАНИЯ И ТРАНСАЛКИЛИРОВАНИЯ

Предложена каталитическая композиция для алкилирования или транслирования ароматических соединений, состоящую из бета цеолита как такового или модифицированного с помощью изоморфного замещения алюминия бором, железом или гелием или путем введения щелочных/щелочно-земельных металлов вслед за процессами ионного обмена, и неорганического лиганда, где экстрацеолитовая пористость, т.е пористость, полученная добавлением фракций мезопористости и макропористости присутствующих в самой каталитической композиции, является такой, что фракция по крайней мере на 25% состоит из пор с радиусом выше. Кроме того, заявлены способы алкилирования и трансалкилирования ароматических углеводородов, которые осуществляют в присутствии вышеупомянутой каталитической композиции.

СПОСОБ ПОЛУЧЕНИЯ БАЗОВОГО СОСТАВА СМАЗОЧНОГО МАСЛА

... 1. Способ получения базового состава смазочного масла, включающийпервую стадию приведения в контакт исходных материалов, содержащих нормальные парафины, имеющие не менее 20 атомов углерода, с первым катализатором в присутствии молекулярного водорода с получением первого получаемого масла, ивторую стадию приведения в контакт первого получаемого масла со вторым катализатором в присутствии молекулярного водорода с получением второго получаемого масла, гдепервый катализатор содержит первый носитель, в котором доля количества NH, которое десорбируется при 300-800°C, в расчете на общее количество NH, которое может десорбироваться, составляет 80-90%, при десорбции NHс программируемым изменением температуры; первый металл, который представляет собой по меньшей мере один металл, выбранный из металлов, которые принадлежат к Группе VI Периодической таблицы, и нанесенный на первый носитель; и второй металл, который представляет собой по меньшей мере один металл, выбранный из металлов, которые принадлежат ...

Kohlenwasserstoffhydrobehandlungskatalysatoren und Verfahren zu ihrer Herstellung

Katalysatorträger

Offenporiger Katalysatorträger, bestehend aus einem Material, welches ein natürliches Schichtsilikat sowie ZrO 2 in tetragonaler Modifikation umfasst. Open-pore catalyst support, consisting of a material comprising a natural sheet silicate and ZrO 2 in tetragonal modification.

Katalysatorsystem

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

Katalysator und Verfahren zur Reinigung von Stoffströmen

FORTSCHREITEN IN DER DEHYDRIERUNGSKATALYSE

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

Hydrogenolyse von Furfurylalkohol zu 1,2-Pentandiol

Diese Erfindung betrifft ein Verfahren zur Herstellung von 1,2-Pentandiol, welches dadurch gekennzeichnet ist, dass man Furfurylalkohol mit Wasserstoff in Gegenwart eines Katalysatorsystems umsetzt. Das Katalysatorsystem kann dabei Platinoxid sein oder Ruthenium, welches auf Aluminiumoxid oder Aktivkohle geträgert ist. Die Erfindung betrifft auch die jeweiligen Katalysatoren sowie Verfahren zu deren Herstellung.

AUS ALUMINIUMTRIHYDRAT HERGESTELLTE ALUMINIUMOXID-VERBUNDSTOFFE MIT HOHEM PORENVOLUMEN UND HOHER SPEZIFISCHER OBERFLÄCHE, DEREN HERSTELLUNG UND VERWENDUNG

Leitfähige Wabenstruktur

Eine leitfähige Wabenstruktur, die enthält:einen säulenförmigen leitfähigen Wabenstrukturabschnitt, der aufweisteine äußere Umfangsseitenwand; undTrennwände, die innerhalb der äußeren Umfangsseitenwand angeordnet sind und die mehrere Zellen definieren, um Strömungswege zu bilden, so dass ein Fluid durch eine erste Stirnfläche in die Strömungswege eintreten und durch eine zweite Stirnfläche austreten kann;wobei ein Paar von Elektrodenschichten, die sich in einer Strömungswegrichtung der Zellen erstrecken, einen Abschnitt einer Außenfläche der äußeren Umfangsseitenwand bildet,eine Elektrodenschicht des Paars von Elektrodenschichten auf einer Seite angeordnet ist, die über eine Mittelachse des Wabenstrukturabschnitts der anderen Elektrodenschicht gegenüberliegt, und,wenn die Wabenstruktur in der Strömungswegrichtung der Zellen in vier gleiche Abschnitte aufgeteilt ist, um vier Bereiche A, B, C und D von einer Seite näher bei der ersten Stirnfläche zu bilden, und ein Durchschnittswert der elektrischen ...

CATALYSTS

Two stage catalytic hydroprocessing of heavy hydrocarbon feedstocks

Heavy hydrocarbon feedstocks are hydroprocessed using a synergistic two-stage catalyst combination. The first stage catalyst comprises at least one Group VIb or Group VIII metal, metal oxide, or metal sulfide on a refractory porous support and has an average pore diameter of 60-150 ANGSTROM . The second stage catalyst comprises at least one Group VIb or VIII metal, metal oxide, or metal sulfide on a refractory porous catalyst support and has an average pore diameter of 30- 70 ANGSTROM and smaller than that of the first stage catalyst. Preferably the first stage catalyst has at least 40% pore volume present as pores having diameters greater than 80 ANGSTROM and the second stage catalyst has at least 50% pore volume present as pores having diameters smaller than 80 ANGSTROM .

Catalyst for steam reforming of hydrocarbons

A catalyst for steam reforming of hydrocarbons comprises porous aluminum oxide and nickel oxide, characterized in that the porous aluminum oxide in which the pore volume given by the pores of the pore diameter ranging from 60 to 120 A is not less than 0.35 ml./g. and the pore volume given by the pores of the pore diameter of more than 120 A is not less than 0.1 ml./g. and the purity determined upon ignition dryness is not less than 98% by weight is impregnated with nickel in an amount ranging from 10 to 30% by weight, as converted to nickel oxide basis, based on the total amount by weight of the catalyst.

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

Selective hydrogenizing process of the diolefines.

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

PROCEDURE FOR THE RECOVERY OF RUTHENIUM CATALYSTS FOR THE NUCLEAR HYDROGENATION OF PHTHALATEN

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

VERFAHREN ZUR SELEKTIVEN HYDRIERUNG VON C2- -MINUS-FRAKTIONEN

VERFAHREN ZUR HERSTELLUNG EINES POROESEN ALUMINIUMOXIDS

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

PROCEDURE FOR THE PRODUCTION OF A POROUS ALUMINA

HYDROGENATION PROCEDURE

HYDROENTMETALLISIERUNG AND HYDRAULIC DESULPHURISATION WITH A CATALYST WITH SPECIFIED MACRO POROSITY.

NICKEL SILICA CATALYST, ITS PRODUCTION AND USE.

CATALYSTS.

PRESSLINGE ON BASIS ALUMINA, PROCEDURE FOR YOUR PRODUCTION, MANUFACTURED BY PYROGEN, AND YOUR USE.

HYDROGENATION CATALYST OF POLYMERS.

MILD ONE HYDROCRACKUNG WITH A CATALYST OF A LIMITED PORE DISTRIBUTION.

PROCEDURE FOR THE PRODUCTION OF HYDROGENATION CATALYSTS

PROCESS FOR THE PREPARATION OF VINYL ACETATE

A silicon-containing alumina support, preparation thereof and a catalyst comprising the alumina support

Method for producing fatty acid alkyl esters

HYDRO PROCESSING OF HYDROCARBON USING A MIXTURE OF CATALYSTS

Hydro processing of hydrocarbon using a mixture of catalysts

Systems, methods, and catalysts for producing a crude product

CATALYST CARRIERS

DEMETALLATION AND DESULFURIZATION OF HEAT HYDROCARBONS

ALUMINIUM PHOSPHATE AND CHROMIUM CATALYST FOR GAS PHASE FLUORIDATION

Coatings

The invention provides a coating composition suitable for use in forming a coating that can reduce the concentration of pollutant gases in the environment, the coating composition comprising polymeric material together with mesoporous titania particles. The particles have a continuous exterior convex surface and a particle diameter of greater than or equal to 1μm but less than or equal to 50μm, and a BET specific surface area of from 30m ...

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

HYDROCONVERSION OF COAL

Process for hydrotreating heavy hydrocarbon oil

SYSTEMS, METHODS, AND CATALYSTS FOR PRODUCING A CRUDE PRODUCT

Contact of a crude feed with one or more catalysts produces a total product that include a crude product. The crude product is a liquid mixture at 25 ~C and 0.101 MPa. One or more other properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

HYDROCARBONS HYDROPROCESSING WITH HALLOYSITE CATALYST

SYSTEMS, METHODS, AND CATALYSTS FOR PRODUCING A CRUDE PRODUCT

... ²²²Contact of a crude feed with one or more catalysts produces a total product ²that include a crude product. The crude product is a liquid mixture at 25 ~C ²and 0.101 Mpa. One or more other properties of the crude product may be ²changed by at least 10 % relative to the respective properties of the crude ²feed.² ...

SYSTEMS, METHODS, AND CATALYSTS FOR PRODUCING A CRUDE PRODUCT

... ²²²Contact of a crude feed with one or more catalysts produces a total product ²that include a crude product. The crude product is a liquid mixture at 25 ~C ²and 0.101 Mpa. One or more other properties of the crude product may be ²changed by at least 10 % relative to the respective properties of the crude ²feed.² ...

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.

CATALYSTS HAVING SELECTED PORE SIZE DISTRIBUTIONS, METHOD OF MAKING SUCH CATALYSTS, METHODS OF PRODUCING A CRUDE PRODUCT, PRODUCTS OBTAINED FROM SUCH METHODS, AND USES OF PRODUCTSOBTAINED

A catalyst and a method of preparation of said catalyst is described herein. The catalyst includes one or more met-als from Columns 6-10 of the Periodic Table and/or one or more compounds of one or more metals from Columns 6-10 of the Pe-riodic Table, a pore size distribution with a median pore diameter ranging from 105 A to 150 A, with 60% of the total number of pores in the pore size distribution having a pore diameter within 60 A of the median pore diameter, with at least 50% of its pore volume in pores having a pore diameter of at most 600 A, and between 5% and 25% of its pore volume in pores having a pore di-ameter between 1000 A and 5000 A. Methods of producing said catalyst are described herein. Crude products and products made from said crude products are described herein.

PROCESS FOR PRODUCING NARROW-PORE CATALYST SUPPORTS

K 2465 PROCESS FOR PRODUCING NARROW-PORE CATALYST SUPPORTS A process for the preparation of narrow-pore alumina supports having surface areas above 300 m2/g, at least 80% of the pore diameters less than 5 nm, a crush strength greater than 88 N and containing an amount of phosphorus in the range from 0.1% to 4.5% by weight, which process comprises: a) precipitating an acid aluminium salt in an aqueous solution in the presence of a phosphorus-containing compound by contact with a basic aluminium compound, b) aging the precipitate at a temperature in the range between 20 .degree.C and 90 .degree.C for at least 15 minutes at a pH in the range between 9.0 to 11.0, c) washing the precipitate, d) drying the precipitate, and e) calcining the precipitate at a temperature ranging from 300 .degree.C to 900 .degree.C. DDR4H04 ...

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.

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 > ...

CATALYST FOR SELECTIVE HYDROGENATION OF ALKYNES IN THE PRESENCE OF DIENES

A catalyst for the hydrogenation of alkynes has a gamma alumina support carrying copper metal and optionally an activator metal. The catalysts of the invention have surprising high selectivity for alkynes, to the relative exclusion of alkenes. The catalyst are advantageously employed for the removal of alkynes (such as 1-butyne-3-ene) from a diene (such as 1,3-butadiene) with relatively little degradation of the diene.

CATALYST FOR REMOVING NITROGEN OXIDES IN EXHAUST GASES

Title of the Invention: CATALYST FOR REMOVING NITROGEN OXIDES IN EXHAUST GASES A catalyst for removing nitrogen oxides in an exhaust gas, said catalyst containing a first group of many pores having a diameter of 1 x 102 .ANG. to less than 1 x 103 .ANG. and a second group of many pores having a diameter of 1 x 103 .ANG. to 1.2 x 105 .ANG., the pore volume of the first group being at least 10% based on the total pore volume of the first group and the second group, and said catalyst comprising titanium and at least one metal selected from molybdenum, tungsten and vanadium as metal elements of catalytically active ingredients.

HYDROTREATMENT PROCESS EMPLOYING CATALYST WITH SPECIFIED PORE SIZE DISTRIBUTION

HYDROTREATMENT PROCESS EMPLOYING CATALYST WITH SPECIFIED PORE SIZE DISTRIBUTION (D#78,764-F) A process for the hydrotreatment of a sulfur and metal-containing hydrocarbon feed comprises contacting said feed with hydrogen and a catalyst in a manner such that the catalyst is maintained at isothermal conditions and is exposed to a uniform quality of feed, where said catalyst has a composition comprising 3.0-5.0 wt. % of an oxide of a Group VIII metal, 14.5-24.0 wt. % of an oxide of a Group VIB metal and 0-2.0 wt. % of an oxide of phosphorus supported on a porous alumina support, and said catalyst is further characterized by having a total surface area of 150-210 m2/g and a total pore volume of 0.50-0.75 cc/g with a pore diameter distribution such that micropores having diameters of 100-160A constitute 70-85% of the total pore volume of said catalyst and macropores having diameters of greater than 250A constitute 5.5-22.0% of the total pore volume of said catalyst. The process of the instant ...

TWO-STAGE HYDROPROCESSING PROCESS AND CATALYST

The present invention pertains to a method for hydroprocessing a heavy hydrocarbon oil, comprising bringing a heavy hydrocarbon oil in a first stage into contact with hydroprocessing catalyst I in the presence of hydrogen, after which the effluent of the first stage is contacted in whole or in part with hydroprocessing catalyst II in the presence of hydrogen, wherein catalyst I comprises 7 to 20 wt. % of a Group VIB metal component, calculated as trioxide on the weight of the catalyst, and 0.5 to 6 wt.% of a Group VIII metal component, calculated as oxide on the weight of the catalyst, on a porous inorganic carrier, said catalyst having a specific surface area of at least 100 m2~/g, a total pore volume of at least 0.55 ml/g, at least 50% of the total pore volume in pores with a diameter of at least 20 nm (200 .ANG.) and at least 65% of the total pore volume in pores with a diameter of 10-120 nm (100-1200 .ANG.), and catalyst II comprises 7 to 20 wt.% of a Group VIB metal component calculated ...

HYDROPROCESSING CATALYST AND PROCESS FOR HYDROPROCESSING HYDROCARBON FEEDS WITH SAID CATALYST

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

REFORMING CATALYST AND A HYDROCARBON CATALYTIC REFORMING PROCESS USING THE CATALYST

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

FCC CATALYST WITH ENHANCED MESOPOROSITY, ITS PREPARATION AND USE

Process for the preparation of a catalyst and a catalyst comprising enhanced mesoporosity is provided herein. Thus, in one embodiment, provided is a particulate FCC catalyst comprising 2 to 50 wt% of one or more ultra stabilized high Si02/A1203 ratio large pore faujasite zeolite or a rare earth containing USY, 0 to 50 wt % of one or more rare-earth exchanged large pore faujasite zeolite, 0 to 30wt% of small to medium pore size zeolites, 5 to 45 wt% quasi-crystalline boehmite 0 to 35 wt% microcrystalline boehmite, 0 to 25 wt% of a first silica, 2 to 30 wt% of a second silica, 0.1 to 10 wt% one or more rare earth components showiomg enhanced mesoporosity in the range of 6 - 40 nm, the numbering of the silica corresponding to their orders of introduction in the preparation process.

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.

METHODS OF PRODUCING A CRUDE PRODUCT

Methods for conversion of a hydrocarbon feed to a total product are described. A hydrocarbon feed is contacted with one or more catalysts to produce the total product. The total product includes a crude product that is a liquid mixture at 25 °C and 0.101 MPa having a residue content of at most 90% of the residue content of the hydrocarbon feed.

SYSTEMS, METHODS, AND CATALYSTS FOR PRODUCING A CRUDE PRODUCT

... ²²²Contact of a crude feed with one or more catalysts produces a total product ²that include a crude product. The crude product is a liquid mixture at 25 ~C ²and 0.101 MPa. One or more other properties of the crude product may be ²changed by at least 10 % relative to the respective properties of the crude ²feed.² ...

NOVEL RESID HYDROTREATING CATALYST

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

HYDROCARBON COMPOSITION WITH HIGH NI/FE/V CONTENT

A catalyst and a method of preparation of said catalyst is described herein. The catalyst includes one or more metals from Columns 6-10 of the Periodic Table and/or one or more compounds of one or more metals from Columns 6-10 of the Periodic Table, a pore size distribution with a median pore diameter ranging from 105 .ANG. to 150 .ANG., with 60% of the total number of pores in the pore size distribution having a pore diameter within 60 .ANG. of the median pore diameter, with at least 50% of its pore volume in pores having a pore diameter of at most 600 .ANG., and between 5% and 25% of its pore volume in pores having a pore diameter between 1000 .ANG. and 5000 .ANG.. Methods of producing said catalyst are described herein. Crude products and products made from said crude products are described herein.

ALUMINA BOUND CATALYST FOR SELECTIVE CONVERSION OF OXYGENATES TO AROMATICS

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

CATALYST FOR SELECTIVE CONVERSION OF OXYGENATES TO AROMATICS

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

CARBON POWDER FOR CATALYST, CATALYST, ELECTRODE CATALYST LAYER, MEMBRANE ELECTRODE ASSEMBLY, AND FUEL CELL USING THE CARBON POWDER

The present invention provides a carbon powder, which can provide a catalyst with superior durability, and a catalyst. This carbon powder for a catalyst has carbon as the principal component and is characterized in that the BET specific surface area per unit weight is 900 m2/g or greater, and a ratio R' (D'/G intensity ratio) of the peak intensity (D' intensity) for the D' band measured in the vicinity of 1620 cm-1 to a peak intensity (G intensity) for the G band measured in the vicinity of 1580 cm-1 by Raman spectrometry is 0.6 or less.

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.

METHOD FOR OXYGENATE CONVERSION

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

METHOD FOR PRODUCING FUEL OIL

Provided is a method that is for producing fuel oil and that can cheaply and highly efficiently produce a fuel oilor starting material thereofhaving as the primary component n-paraffin or isoparaffin from a starting material oil containing a fatty acid alkyl ester, even while reducing hydrogen pressure. The method for producing fuel oil has a step for producing fuel oil having one or both of n-paraffin and isoparaffin as the primary component by contacting hydrogen gas and a starting material oil containing a fatty acid alkyl ester under the condition of a hydrogen pressure of no greater than 1 MPa to a catalyst resulting from supporting on a porous metal oxide support one or more metal elements belonging to group nine or group ten of the periodic table, and one or more group six element oxides belonging to group six of the periodic table. The weight ratio of the group six elements to the metal elements contained in the catalyst is no greater than 1.0 in terms of the metal.

HYDROPROCESSING CATALYST COMPOSITION

Hydroprocessing catalysts which comprise alumina and Group VIB and VIII metal components having a desired pore size/volume distribution and high surface area, i.e. above 330 m2/g.

PROCESS

NOVEL PROCESS D#79,143 -F Hydrodesulfurization and demetallalization of hydrocarbon charge is effected by hydrogenation in the presence of, as catalyst, a Group VI A metal and a non-noble Group VIII metal on a trimodal alumina support.

HYDROGENATION CATALYST, PROCESS FOR PREPARING AND PROCESS OF USING SAID CATALYST

In one embodiment, the invention relates to a catalyst in powdered form which comprises a major amount of the oxides of copper and zinc, and a minor amount of aluminum oxide wherein the pore volume of pores of said catalysts having a diameter of greater than about 80A.degree. is at least about 80% of the total pore volume. In another embodiment, the invention relates to a process for preparing hydrogenation catalysts comprising the oxides of copper, zinc and aluminum which comprises the steps of (A) preparing a first aqueous solution containing at least one water-soluble copper salt and at least one water-soluble zinc salt; (B) preparing a second solution containing at least one water-soluble basic aluminum salt and at least one alkaline precipitating agent; (C) mixing the first and second solutions whereby an insoluble solid is formed; (D) recovering the insoluble solid. The invention also relates to a process for hydrogenating aldehydes, ketones, carboxylic acids and carboxylic acid esters ...

PROCESS FOR THE PREPARATION OF VINYL ACETATE

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

A MATERIAL WITH MICROPOROUS CRYSTALLINE WALLS DEFINING A NARROW SIZE DISTRIBUTION OF MESOPORES,AND PROCESS FOR PREPARING SAME

CATALYST AND PROCESS FOR HYDROCRACKING HYDROCARBON FRACTIONS

L'invention concerne un catalyseur d'hydrocraquage renfermant au moins un métal du groupe VIB, et/ou au moins un métal du groupe VIII de la classification périodique, une matrice alumine, du phosphore, éventuellement au moins un élément du groupe VIIA (fluor) et une zéolithe Y non désaluminée globalement de paramètre cristallin supérieur à 2,438 nm, de rapport SiO2/Al2O3 global inférieur à 8, de rapport SiO2/Al2O3 de charpente inférieur à 21 et supérieur au rapport SiO2/Al2O3 global. L'invention concerne également un procédé d'hydrocraquage avec ce catalyseur , notamment aux basses pressions de 7,5 à 11 MPa.

CATALYST AND PROCESS FOR HYDROCRACKING HYDROCARBON FRACTIONS

L'invention concerne un catalyseur d'hydrocraquage renfermant au moins un métal du groupe VIB, et/ou au moins un métal du groupe VIII de la classification périodique, une matrice alumine, du phosphore, éventuellement au moins un élémen t du groupe VIIA (fluor) et une zéolithe Y non désaluminée globalement de paramètr e cristallin supérieur à 2,438 nm, de rapport SiO2/Al2O3 global inférieur à 8, de rapport SiO2/Al2O3 de charpente inférieur à 21 et supérieur au rapport SiO2/Al2O3 global . L'invention concerne également un procédé d'hydrocraquage avec ce catalyseur, notamment aux basses pressions de 7,5 à 11 MPa.

METHODS FOR PRODUCING MULTIFUNCTIONAL CATALYSTS FOR UPGRADING PYROLYSIS OIL

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

METHODS FOR PRODUCING MULTIFUNCTIONAL CATALYSTS FOR UPGRADING PYROLYSIS OIL

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

COMPLEX OXIDE, METHOD FOR PRODUCING SAME, AND EXHAUST GAS PURIFYING CATALYST

Disclosed are a composite oxide which is capable of maintaining a large volume of pores even used in a high temperature environment, and which has excellent heat resistance and catalytic activity, as well as a method for producing the composite oxide and a catalyst for exhaust gas purification employing the composite oxide. The composite oxide contains cerium and at least one element selected from aluminum, silicon, or rare earth metals other than cerium and including yttrium, at a mass ratio of 85:15 to 99:1 in terms oxides, and has a property of exhibiting a not less than 0.30 cm/g, preferably not less than 0.40 cm/g volume of pores with a diameter of not larger than 200 nm, after calcination at 900° C. for 5 hours, and is suitable for a co-catalyst in a catalyst for vehicle exhaust gas purification. 1. A composite oxide comprising (A) cerium and (B) at least one element selected from the group consisting of aluminum , silicon , and rare earth metals other than cerium ,wherein a mass ratio of (A):(B) in the composite oxide is 85:15 to 99:1 in terms oxides, and{'sup': '3', 'wherein the composite oxide has a property of exhibiting a not less than 0.30 cm/g volume of pores with a diameter of not larger than 200 nm, after calcination at 900° C. for 5 hours.'}2. The composite oxide according to claim 1 , having a property of exhibiting a not less than 0.40 cm/g volume of pores with a diameter of not larger than 200 nm claim 1 , after calcination at 900° C. for 5 hours.3. The composite oxide according to claim 1 , having a property of exhibiting a not less than 0.50 cm/g volume of pores with a diameter of not larger than 200 nm claim 1 , after calcination at 900° C. for 5 hours.4. The composite oxide according to claim 1 , having a property of exhibiting a not less than 0.32 cm/g volume of pores with a diameter of not larger than 200 nm claim 1 , after calcination at 800° C. for 5 hours.5. The composite oxide according to claim 1 , comprising at least silicon as (B) ...

SYSTEMS AND METHODS FOR PRODUCING PROPYLENE

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

DUAL CATALYST SYSTEM FOR PROPYLENE PRODUCTION

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

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

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

METALLIC NANOPARTICLE CATALYSTS EMBEDDED IN POROUS OXIDE SUPPORT, WHICH SHOW HIGH CATALYTIC ACTIVITY EVEN AT LOW TEMPERATURES

The present invention relates to a metallic nanoparticle catalyst, and more particularly, to a porous catalyst in which metallic nanoparticles are embedded in a porous oxide support, and a method for preparing the porous catalyst. To this end, a porous catalyst composition having metallic nanoparticles of the present invention includes an oxide matrix structure having mesopores and micropores; and metal or metal oxide nanoparticles embedded in the oxide matrix structure having the mesopores and micropores. Thus, metallic nanoparticle catalysts having high activity even at low temperature are realized. 1. A porous catalyst composition having metallic nanoparticles comprising:an oxide matrix structure having mesopores and micropores; andmetal or metal oxide nanoparticles embedded in the oxide matrix structure having the mesopores and micropores.2. The porous catalyst composition having metallic nanoparticles according to claim 1 ,wherein the metal or metal oxide nanoparticles are non-uniformly or non-hierarchically dispersed.3. A method for preparing a porous catalyst composition having metallic nanoparticles claim 1 , comprising:a step of covering metallic nanoparticles containing at least any one of a metal and a metal oxide with a stabilizer to stabilize the metallic nanoparticles and then binding a polymer to surfaces of the metallic nanoparticles to functionalize the metallic nanoparticles (Step 1);a step of mixing an oxide precursor with a solution in which the functionalized metallic nanoparticles and an activator are mixed and dispersed, thereby synthesizing a metallic nanoparticle dispersion embedded in a porous oxide support (Step 2); anda step of calcining the metallic nanoparticle dispersion (Step 3).4. The method for preparing a porous catalyst composition having metallic nanoparticles according to claim 3 ,wherein a polymer used for the functionalization has a molecular weight selected in a range of 200 to 20 k Da.5. The method for preparing a porous ...

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 ...

Shaped porous 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.

Catalyst System and Use in Heavy Aromatics Conversion Processes

Disclosed are a catalyst system and its use in a process for the conversion of a feedstock containing C 8 + aromatic hydrocarbons to produce light aromatic products, comprising benzene, toluene and xylene. The catalyst system comprises (a) a first catalyst bed comprising a first catalyst composition, said first catalyst composition comprising a zeolite having a constraint index of 3 to 12 combined (i) optionally with at least one first metal of Group 10 of the IUPAC Periodic Table, and (ii) optionally with at least one second metal of Group 11 to 15 of the IUPAC Periodic Table; and (b) a second catalyst bed comprising a second catalyst composition, said second catalyst composition comprising (i) a meso-mordenite zeolite, combined (ii) optionally with at least one first metal of Group 10 of the IUPAC Periodic Table, and (iii) optionally with at least one second metal of Group 11 to 15 of the IUPAC Periodic Table, wherein said meso-mordenite zeolite is synthesized from TEA or MTEA and having a mesopore surface area of greater than 30 m 2 /g and said meso-mordenite zeolite comprises agglomerates composed of primary crystallites, wherein said primary crystallites have an average primary crystal size as measured by TEM of less than 80 nm and an aspect ratio of less than 2.

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. ...

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 ...

METHOD FOR PRODUCING ALCOHOL

A method for producing an alcohol having 8 or more and 22 or less carbon atoms includes the following steps: step 1: forming a porous layer on a surface of a porous material having a pore size mode of 30 nm or more and 200 nm or less to obtain a bimodal carrier; step 2: supporting cobalt on the bimodal carrier obtained in step 1 to obtain a catalyst having peaks of pore distribution in a range of 1 nm or more and 25 nm or less and a range of 30 nm or more and 200 nm or less, respectively; and step 3: reacting carbon monoxide with hydrogen at a gauge pressure of 2 MPa or more and 100 MPa or less in the presence of the catalyst obtained in step 2. 1. A method for producing an alcohol having 8 or more and 22 or less carbon atoms comprising the following steps:step 1: forming a porous layer on a surface of a porous material having a pore size mode of 30 nm or more and 200 nm or less to obtain a bimodal carrier;step 2: supporting cobalt on the bimodal carrier obtained in step 1 to obtain a catalyst having peaks of pore distribution in a range of 1 nm or more and 25 nm or less and a range of 30 nm or more and 200 nm or less, respectively; andstep 3: reacting carbon monoxide with hydrogen at a gauge pressure of 2 MPa or more and 100 MPa or less in the presence of the catalyst obtained in step 2.2. The method for producing an alcohol having 8 or more and 22 or less carbon atoms according to claim 1 , wherein the porous layer contains one or two or more selected from a silicate claim 1 , silicon oxide claim 1 , aluminum oxide claim 1 , and zirconium oxide.3. The method for producing an alcohol having 8 or more and 22 or less carbon atoms according to claim 1 , wherein step 1 comprises the following steps:step 1-1: supporting a dispersion or a solution containing a raw material of the porous layer on the porous material; andstep 1-2: calcining the porous material with the dispersion or the solution supported thereon obtained in step 1-1.4. The method for producing an alcohol ...

PROCESS FOR THE CATALYTIC CONVERSION OF MICRO CARBON RESIDUE CONTENT OF HEAVY HYDROCARBON FEEDSTOCKS AND A LOW SURFACE AREA CATALYST COMPOSITION FOR USE THEREIN

An improved process for the hydroconversion of micro carbon residue content of heavy hydrocarbon feedstocks by the use of a catalyst composition that is especially useful in the conversion of micro carbon residue of such feedstocks. The catalyst composition is a low surface area composition that further has a specifically define pore structure the combination of which provides for its enhance micro carbon residue conversion property. 1. A process for converting at least a portion of an MCR content of a heavy hydrocarbon feedstock to yield a product having a reduced MCR content , wherein said process includes contacting said heavy hydrocarbon feedstock with a catalyst under MCR conversion process conditions and yielding said product , wherein the improvement comprises: enhancing the conversion of said MCR content of said heavy hydrocarbon feedstock by using as said catalyst in said process a calcined particulate of a co-mulled mixture , wherein said co-mulled mixture that is formed into a particulate , which is subsequently calcined to provide said calcined particulate , comprises a molybdenum component , a nickel component , an uncalcined pseudo-boehmite powder prepared by a two-step precipitation process and comprising at least 90 weight percent pseudo-boehmite , a mineral acid , and a catalyst fines portion having a particle size between 5 and 50 microns (μm) and a mean pore diameter between 40 Å and 150 Å , and wherein said calcined particulate is prepared under conditions so that it has specifically defined physical properties including:{'sup': 2', '2, '(a) a total surface area of greater than 160 m/g and less than 240 m/g;'}(b) a median pore diameter in the range of from 85 Å to 120 Å;(c) from 8% to 22% of the total pore volume of said calcined particulate in the macropores having a pore diameter of 250 Å or greater; and(d) greater than 40% and no more than 60% of the total pore volume of said calcined particulate within its pores having a diameter in the range ...

Low-Temperature Oxidation Catalyst With Particularly Marked Hydrophobic Properties For The Oxidation Of Organic Pollutants

The present invention relates to a catalyst comprising a macroporous noble metal-containing zeolite material and a porous SiO-containing binder, wherein the catalyst has a proportion of micropores of more than 70%, based on the total pore volume of the catalyst. The invention is additionally directed to a process for preparing the catalyst and to the use of the catalyst as an oxidation catalyst. 19.-. (canceled)10. Method of producing a catalyst according to , comprising the following steps:a) introducing a noble metal precursor compound into a microporous zeolite material;b) calcining the zeolite material loaded with the noble metal precursor compound;{'sub': '2', 'c) mixing the zeolite material loaded with the noble metal compound with a porous SiO-containing binder and a solvent;'}d) drying and calcining the mixture comprising the zeolite material loaded with the noble metal compound and the binder.11. Method according to claim 10 , wherein the mixture obtained in step c) is applied to a support.12. (canceled) The present invention relates to a catalyst comprising a microporous noble metal-containing zeolite material and a porous SiO-containing binder, wherein the catalyst has a proportion of micropores of more than 70%, relative to the total pore volume of the catalyst. The invention is additionally directed to a method of producing the catalyst as well as to the use of the catalyst as oxidation catalyst.Purifying exhaust gases by means of catalysts has been known for some time. For example, the exhaust gases from combustion engines are purified with so-called three-way catalysts (TWC). The nitrogen oxides are reduced with reductive hydrocarbons (HC) and carbon monoxide (CO).Likewise, the exhaust gases from diesel engines are post-treated with catalysts. Here, carbon monoxide, unburnt hydrocarbons, nitrogen oxides and soot particles, for example, are removed from the exhaust gas. Unburnt hydrocarbons which are to be treated catalytically include paraffins, ...

MESOPOROUS MATERIALS

The invention relates to the field of mesoporous materials and in particular to mesoporous rare earth oxides and a method of their synthesis. 1. A method of making a mesoporous rare earth oxide material , the method comprising;at a reduced pressure, contacting a mesoporous template with a precursor solution that comprises a rare earth metal salt or neutral complex of a rare earth metal, so as to impregnate the mesoporous template;calcining the impregnated mesoporous template to form a rare earth oxide material in situ; andremoving the mesoporous template from the calcined material.2. A method according to claim 1 , comprising contacting the mesoporous template with a non-aqueous precursor solution so as to impregnate the mesoporous template3. A method according to claim 2 , wherein the precursor solution comprises ethanol as a solvent.4. A method according to any preceding claim claim 2 , wherein the precursor solution comprises cerium.5. A method according to any preceding claim claim 2 , wherein the precursor solution is a saturated solution claim 2 , optionally comprising more than 20 wt % of precursor salt.6. A method according to any preceding claim claim 2 , comprising calcining at more than one temperature.7. A method according to claim 6 , comprising calcination at a first temperature for a first period of time and at a higher second temperature for a second period of time.8. A method according to any preceding claim claim 6 , comprising chemically removing the mesoporous template claim 6 , by treating with a chemical capable of eroding or digesting the template.9. A method according to claim 8 , wherein the mesoporous template is a silicate material claim 8 , the method comprising treatment with aqueous alkali metal hydroxide at room temperature.10. A method according to claim 9 , wherein the aqueous alkali metal hydroxide is NaOH(aq) and has a concentration of between around 1-3 M.11. A method according to any preceding claim claim 9 , wherein the method ...

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 ...

Mesoporous Carbon Modified with Polyethylenimine Catalysis Bisphenol A in Organic Solvent

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

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

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

Multi-metallic Catalyst System And Use Of The Same In Preparing Upgraded Fuel From Biomass

The present disclosure provides a multi-metallic catalyst system comprising at least one support, and at least one promoter component and an active component comprising at least two metals uniformly dispersed on the support. The present disclosure also provides a process for preparing the multi-metallic catalyst system. Further, the present disclosure provides a process for preparing upgraded fuel from biomass. The process is carried out in two steps. In the first step, a biomass slurry is prepared and is heated in the presence of hydrogen and a multi-metallic catalyst that comprises at least one support, at least one promoter component, and an active component comprising at least two metals to obtain crude biofuel as an intermediate product. The intermediate product obtained in the first step is then cooled and filtered to obtain a filtered intermediate product. In the second step, the filtered intermediate product is hydrogenated in the presence of the multi-metallic catalyst to obtain the upgraded fuel. The fuel obtained from the process of the present disclosure is devoid of heteroatoms such as oxygen, nitrogen and sulfur. 1. A multi-metallic catalyst system comprising:i. at least one alumina support;ii. a promoter component impregnated on said at least one support; wherein said promoter is at least one selected from the group consisting of Niobium (Nb) and Phosphorous (P); andiii. an active component comprising cobalt and molybdenum, being uniformly dispersed on said at least one support.2. The catalyst system as claimed in claim 1 , wherein said catalyst system is characterized by having BET surface area in the range of 165 to 170 m/g claim 1 , pore volume in the range of 0.48 to 0.50 cc/g claim 1 , pore width in the range of 78 to 82 Å claim 1 , and total acidity in the range of 0.810 to 0.812 mmol/g.3. The catalyst system as claimed in claim 1 , wherein said support is in at least one form selected from the group consisting of spheres claim 1 , extrudates ...

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

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

HYDROISOMERIZATION CATALYST WITH A BASE EXTRUDATE HAVING A LOW PARTICLE DENSITY

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

HYDROISOMERIZATION CATALYST MANUFACTURED USING A HIGH NANOPORE VOLUME ALUMINA SUPPORTS

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

EXHAUST GAS PURIFICATION CATALYST

The present invention provides an exhaust gas purification catalyst provided with: a substrate of wall flow structure in which inlet cells and outlet cells are partitioned by porous partition walls; and a catalyst layer disposed at least inside the partition wall and including a catalyst body. The catalyst layer satisfies the following conditions: (1) the pore volume of pores no larger than 5 μm, as measured in accordance with a mercury intrusion technique, is 24000 mmor greater per L of volume of the substrate; and (2) a permeability coefficient measured by a Perm porometer is 0.6 μmto 4.4 μm. 1. An exhaust gas purification catalyst disposed in an exhaust path of an internal combustion engine and configured to purify exhaust gas emitted by the internal combustion engine , the exhaust gas purification catalyst comprising:a substrate of wall flow structure where an inlet cell in which an exhaust gas inflow end section is open and an exhaust gas outflow end section is closed, and an outlet cell in which an exhaust gas outflow end section is open and an exhaust gas inflow end section is closed, are partitioned by a porous partition wall; anda catalyst layer disposed at least inside the partition wall and including a catalyst body,wherein the catalyst layer satisfies the following conditions:{'sup': '3', '(1) in a relationship between a pore size and a pore volume based on a pore distribution measured in accordance with a mercury intrusion technique, the pore volume of pores no larger than 5 μm is 24000 mmor greater per L of volume of the substrate; and'}{'sup': 2', '2, '(2) a permeability coefficient measured by a Perm porometer is 0.6 μmto 4.4 μm.'}2. The exhaust gas purification catalyst according to claim 1 , wherein the permeability coefficient is 1.9 μmor larger.3. The exhaust gas purification catalyst according to claim 2 , wherein the permeability coefficient is 2.4 μmor smaller.4. The exhaust gas purification catalyst according to claim 1 , wherein the pore ...

PROCESSES FOR THE PREPARATION OF MESOPOROUS METAL OXIDES

A process for preparing a crystalline mesoporous metal oxide, i.e., crystalline mesoporous transition metal oxide, crystalline mesoporous Lanthanide metal oxide, a crystalline mesoporous post-transition metal oxide and crystalline mesoporous metalloid oxide. The process comprises providing an acidic mixture comprising an amorphous mesoporous metal oxide; and heating the acidic mixture at a temperature and for a period of time sufficient to form the crystalline mesoporous metal oxide. A crystalline mesoporous metal oxide prepared by the above process. A method of controlling nano-sized wall crystallinity and mesoporosity in crystalline mesoporous metal oxides. The method comprises providing an acidic mixture comprising an amorphous mesoporous metal oxide; and heating the acidic mixture at a temperature and for a period of time sufficient to control nano-sized wall crystallinity and mesoporosity in the mesoporous metal oxides. Crystalline mesoporous metal oxides and a method of tuning structural properties of mesoporous metal oxides. 1. A process for preparing a crystalline mesoporous metal oxide , said process comprising:providing an acidic mixture comprising an amorphous mesoporous metal oxide; andheating the acidic mixture at a temperature and for a period of time sufficient to form the crystalline mesoporous metal oxide.2. The process of claim 1 , wherein the acidic mixture is heated at a temperature less than about 80° C. for a period less than about 2 hours.3. The process of claim 1 , wherein the acidic mixture comprises an aqueous acidic solution less than or equal to 0.5 M H or less than or equal to 0.5 M K.4. The process of claim 1 , wherein the acidic mixture is heated at a temperature less than about 70° C. for a period less than about 1.5 hours.5. The process of claim 1 , wherein the acidic mixture comprises an aqueous acidic solution less than or equal to 0.4 M H or less than or equal to 0.4 M K.6. The process of claim 1 , wherein the amorphous mesoporous ...

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 AND PROCESS FOR THE SELECTIVE CONVERSION OF HYDROCARBONS

A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with a median diameter between 1.6 mm and 2.5 mm and an apparent bulk density between 0.6 and 0.3 g/cc. Also a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same. 1. A catalyst for a selective conversion of hydrocarbons , the catalyst comprising:a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof; anda support forming a catalyst particle, the catalyst particle comprising a plurality of pores, a median diameter between 1.6 mm and 2.5 mm, and an apparent bulk density between 0.6 and 0.3 g/cc,{'sup': −6', '2', '−7', '2, 'wherein the catalyst particle has an effective carbon dioxide diffusivity at 10° C. of at least 1.6×10m/sec, or has an oxygen effective diffusivity at 480° C. of at least 1.5×10m/s, or has both.'}2. The catalyst of wherein the apparent bulk density is between 0.6 and 0.5 g/cc.3. The catalyst of wherein the median diameter is between 1.8 mm and 2.2 mm.4. The catalyst of wherein the median diameter is between 1.8 mm and 2.2 mm.5. The catalyst of wherein the apparent bulk density is between 0.57 to 0.52 g/cc.6. The catalyst of wherein the median diameter is 1.8 mm.7. The ...

CATALYST AND PROCESS FOR THE SELECTIVE CONVERSION OF HYDROCARBONS

A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with an average pore diameter between 200 to 350 Angstroms, a porosity of at least 75% and an apparent bulk density between 0.60 and 0.3 g/cc. Also, a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same. 1. A catalyst for a selective conversion of hydrocarbons , the catalyst comprising:a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof; anda support forming a catalyst particle comprising a plurality of pores, wherein at least 15% of the pores have an average pore diameter between 200 to 350 Angstroms, and wherein the catalyst particle has an apparent bulk density between 0.60 and 0.3 g/cc.2. The catalyst of wherein the apparent bulk density is between 0.60 and 0.5 g/cc.3. The catalyst of wherein the apparent bulk density is between 0.57 to 0.52 g/cc.4. The catalyst of wherein the wherein the apparent bulk density is 0.57 g/cc.5. The catalyst of wherein the at least 15% of the pores having an average pore diameter between 200 to 350 Angstroms have an average pore diameter between 240 to 280 Angstroms.6. The catalyst of wherein the catalyst has mono-modal porous distribution.7. The catalyst ...

Processes for regenerating a catalyst for the selective conversion of hydrocarbons

A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with an average pore diameter between 200 to 350 Angstroms, a porosity of at least 75% and an apparent bulk density between 0.60 and 0.3 g/cc. Also, a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same.

PROCESSES FOR REGENERATING A CATALYST FOR THE SELECTIVE CONVERSION OF HYDROCARBONS

A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with a median diameter between 1.6 mm and 2.5 mm and an apparent bulk density between 0.6 and 0.3 g/cc. Also a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same. 1. A process for reducing a time associated with regenerating a catalyst used for a selective conversion of hydrocarbons , the process comprising:removing coke from a catalyst comprising a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof, and wherein the time associated with regenerating the catalyst is reduced at least 10% compared to a theoretical time for regenerating the catalyst by the catalyst further comprising a support forming a catalyst particle with a median diameter between 1.6 mm and 2.5 mm and an apparent bulk density between 0.6 and 0.3 g/cc.2. The process of wherein the apparent bulk density is between 0.6 and 0.5 g/cc.3. The process of wherein the median diameter is between 1.8 mm and 2.2 mm.4. The process of wherein the median diameter is between 1.8 mm and 2.2 mm.5. The process of wherein the apparent bulk density is between 0.57 to 0.52 g/cc.6. The process of wherein the median diameter is 1.8 mm.7. The process ...

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 Material And Devices For Performing Separations, Filtrations, And Catalysis And EK Pumps, And Mthods Of Making And Using The Same

Embodiments of the present invention are directed to a porous monolith polymeric composition having utility in catalysis, chromatography, filtration, and electro-kinetic pumps, devices incorporating such composition and methods or making and using such monoliths. The monoliths are characterized by a substantially homogeneous skeletal core with little shrinkage, few voids and few channels. 1. A composition of matter comprising a monolith having a skeletal core and pores , said skeletal core having a substantially homogeneous polymeric composition of two or more organic silane monomers , said pores defining an interstitial volume in the skeletal core and have a pore size distribution in which there are at least macropores and less than 5% of the interstitial volume is mesopores , said macropores allowing fluid movement through the monolith.2. The composition of matter of in which said interstitial volume has fewer than 2% mesopores.3. The composition of matter of wherein said interstitial volume has fewer than 1% mesopores.4. The composition of matter of wherein said skeletal core has polymers which deviate from the substantially homogeneous polymeric composition to form nodules claim 1 , said nodules have a nodule cross-sectional diameter and said skeletal core having a substantially homogeneous polymeric composition without a nodule has a core cross-sectional diameter wherein the ratio of the nodule cross sectional diameter to core cross sectional diameter is less than 80 to 1.5. The composition of matter of wherein said skeletal core has polymers which deviate from the substantially homogeneous polymeric composition to form nodules claim 1 , said nodules have a nodule cross-sectional diameter and said skeletal core claim 1 , having a substantially homogeneous polymeric composition without a nodule claim 1 , has a core cross-sectional diameter wherein the ratio of the nodule cross sectional diameter to core cross sectional diameter is less than 50 to 1.6. The ...

POROUS BODIES WITH ENHANCED PORE ARCHITECTURE

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

POROUS MATERIAL AND DEVICES FOR PERFORMING SEPARATIONS, FILTRATIONS, AND CATALYSIS AND EK PUMPS, AND METHODS OF MAKING AND USING THE SAME

Embodiments of the present invention are directed to a porous monolith polymeric composition having utility in catalysis, chromatography, filtration, and electro-kinetic pumps, devices incorporating such composition and methods or making and using such monoliths. The monoliths are characterized by a substantially homogeneous skeletal core with little shrinkage, few voids and few channels. 154.-. (canceled)56. The composition of matter of wherein said aliphatic groups are lower alkyl groups.57. The composition of matter of wherein said aliphatic groups are methyl claim 55 , ethyl claim 55 , propyl claim 55 , butyl claim 55 , pentyl claim 55 , hexyl claim 55 , heptyl and octyl.58. The composition of matter of wherein said first monomer is methyltrimethoxysilane.59. The composition of matter of wherein said second monomer is dimethyldimethoxysilane.60. The composition of matter of wherein said third monomer is tetramethoxysilane.61. The composition of matter of wherein said third monomer is bis(trimethoxysilyl)ethane.62. The composition of matter of wherein said first monomer claim 55 , second monomer and third monomer define proportions of the skeletal core of 10-15 parts first monomer claim 55 , 1-10 parts second monomer and 0.5 to 5 parts third monomer.63. The composition of matter of wherein said monolith has a skeletal volume and a pore volume claim 55 , said pore volume and skeletal volume forming a monolith volume which monolith volume exhibits less than 1% shrinkage as said monolith is formed in a polymerization reaction.64. The composition of matter of wherein said skeletal core has a core mass and a skeletal volume and said pores have a pore volume which core mass claim 55 , skeletal volume and pore volume define a density claim 55 , and such density varies by less than 5% throughout said monolith.65. The composition of matter of wherein said skeletal core has polymers which deviate from the substantially homogeneous polymeric composition to form nodules ...

Process for the commercial production of high-quality catalyst materials

The present invention describes an improved process for the commercial scale production of high-quality catalyst materials. These improved processes allow for production of catalysts that have very consistent batch to batch property and performance variations. In addition these improved processes allow for minimal production losses (by dramatically reducing the production of fines or small materials as part of the production process). The improved process involves multiple steps and uses calcining ovens that allow for precisely control temperature increases where the catalyst is homogenously heated. The calcining gas is released into a separate heating chamber, which contains the recirculation fan and the heat source. Catalysts that may be produced using this improved process include but are not limited to catlaysts that promote CO hydrogenation, reforming catalysts, Fischer Tropsch Catalysts, Greyrock GreyCat™ catalysts, catalysts that homologate methanol, catalysts that promote hydrogenation of carbon compounds, and other catalysts used in industry. 1. A catalyst production process wherein catalyst materials are heated homogeneously in an calcining oven and in which the oven heating and gas flow rates are controlled , resulting in the production of catalysts that meet batch-to-batch chemical , physical and performance specifications with a high level of reproducibility , wherein the process comprises the steps of:a. Loading catalyst materials into calcining ovens;b. wherein the calcining oven is connected to one or more separate reheating chambers, in which the calcining gas is heated using a thermostatically controlled heat source;c. circulating the heated calcining gas from the reheating chambers into the calcining ovens in which the gas is distributed over catalyst materials;d. recirculating the calcining gas back into the reheating chambers at a recirculation rate as necessary to maintain temperatures homogeneously throughout the calcining oven to within about ...

HIGH METALS CONTENT HYDROLYSIS CATALYST FOR USE IN THE CATALYTIC REDUCTION OF SULFUR CONTAINED IN A GAS STREAM, AND A METHOD OF MAKING AND USING SUCH COMPOSITION

Disclosed is a composition useful in the hydrolysis of sulfur compounds that are contained in a gas stream. The composition comprises a calcined co-mulled mixture of psuedoboehmite, a cobalt compound, and a molybdenum compound such that the composition comprises gamma-alumina, at least 7.5 wt. % molybdenum, and at least 2.75 wt. % cobalt. The composition is made by forming into an agglomerate a co-mulled mixture pseudoboehmite, a cobalt component, and a molybdenum component followed by drying and calcining the agglomerate to provide a catalyst composition comprising gamma-alumina, at least 7.5 wt. % molybdenum, and at least 2.75 wt. % cobalt. 1. A hydrolysis process , comprising: introducing a gas stream , comprising a sulfur compound or carbon monoxide , or both , into a reactor that defines a reaction zone containing a catalyst composition and operated at suitable reaction conditions; and contacting said gas stream with said catalyst composition , wherein said catalyst composition comprises a formed agglomerate of a comulled mixture , comprising pseudobohemite , a cobalt compound and a molybdenum compound , wherein said comulled mixture has been calcined to provide said catalyst composition , comprising gamma-alumina , at least 7.5 wt. % molybdenum; and at least 2.75 wt. % cobalt , wherein each wt. % is based on the total weight of said catalyst composition and the metal as an oxide regardless of its actual form.2. A process as recited in claim 1 , wherein said sulfur compound is present in said gas stream at a sulfur compound concentration in the range of from 0.01 volume % to 2 volume % claim 1 , and wherein said sulfur compound is selected from the group of compounds consisting of carbonyl sulfide (COS) claim 1 , carbon disulfide (CS) claim 1 , sulfur dioxide (SO) claim 1 , and elemental sulfur (S).3. A process as recited in claim 2 , wherein said suitable reduction reaction conditions include an inlet temperature to said reactor that is in the range of from ...

A PROCESS FOR MANUFACTURING AN UPGRADED BIO-OIL FROM BLACK LIQUOR

The present invention relates to a process for manufacturing an upgraded bio-oil derived from black liquor, comprising the following steps: —Providing black liquor, which comes from the pulp and paper manufacturing industry; —Subjecting black liquor to a pyrolysis treatment with formation of a pyrolyzed black liquor gas and a solid mass, which comprises char and salts; —Catalytic conversion of said pyrolyzed black liquor gas by contacting at least part of the latter with a bi-metallic modified zeolite catalyst with formation of the upgraded bio-oil, which comprises benzene, toluene, xylene (BTX), naphthalene and non-BTX products. 1. A process for manufacturing an upgraded bio-oil derived from a black liquor , comprising the following steps:providing the black liquor;subjecting the black liquor to a pyrolysis treatment and forming a pyrolyzed black liquor gas and a solid mass wherein the solid mass; comprises char and salts;forming the upgraded bio-oil, which comprises benzene, toluene, xylene (BTX), naphthalene, and non-BTX products, through catalytic conversion of the pyrolyzed black liquor gas by contacting at least part of the pyrolyzed black liquor gas with a bi-metallic modified zeolite catalyst.2. The process according to claim 1 , wherein a first metal and a second metal are incorporated into said catalyst.3. The process according to claim 1 , wherein said first metal is a transition metal selected from Group IIB of the periodic table and wherein said second metal consists of:a. one metallic element selected from the Lanthanide series of the periodic table having an atomic number ranging from 57 to 60; orb. a transition metal of Group IB of the periodic table; orc. a transition metal of Group VIB of the periodic table.4. The process according to claim 2 , wherein said support catalyst has a silica alumina molar ratio from 5 to 300.5. The process according to claim 2 , wherein the support catalyst has an internal pore size distribution in the range of 4.5 to ...

DUAL CATALYST SYSTEM FOR PROPYLENE PRODUCTION

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

CATALYST AND ITS USE FOR THE SELECTIVE HYDRODESULFURIZATION OF AN OLEFIN CONTAINING HYDROCARBON FEEDSTOCK

A catalyst and its use for selectively desulfurizing sulfur compounds present in an olefin-containing hydrocarbon feedstock to very low levels with minimal hydrogenation of olefins. The catalyst comprises an inorganic oxide substrate containing a nickel compound, a molybdenum compound and optionally a phosphorus compound, that is overlaid with a molybdenum compound and a cobalt compound. The catalyst is further characterized as having a bimodal pore size distribution with a large portion of its total pore volume contained in pores having a diameter less than 250 angstroms and in pores having a diameter greater than 1000 angstroms. 1. A process for selectively hydrodesulfurizing sulfur compounds contained in an olefin-containing hydrocarbon feedstock with minimal hydrogenation of olefins , which process comprises:contacting in a reactor under selective hydrodesulfurization conditions said olefin-containing hydrocarbon feedstock with a calcined catalyst particle made by calcining a shaped particle of a mixture comprising an inorganic oxide support material, molybdenum trioxide and a nickel compound to provide a calcined shaped particle;wherein said calcined shaped particle is further overlaid with a cobalt compound and a molybdenum compound and is subjected to a further calcination step to produce said calcined catalyst particle, said calcined catalyst particle being characterized by having a bimodal pore size distribution with at least 20% of the total pore volume being in pores having a diameter less than 250 angstroms and at least 10% of the total pore volume being in pores having a diameter greater than 1000 angstroms.212. The process as recited in claim , wherein said catalyst has a molybdenum content of from 9 wt % to 23 wt % , a cobalt content of from 2 wt % to 8 wt % , a nickel content of from 0.5 wt % to 2 wt % , and a phosphorus content of from 0.1 wt % to 3.5 wt % , each of said percentages calculated as the element.313. The process as recited in claim , ...

CATALYST SUPPORT AND CATALYSTS PREPARED THEREFROM

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

SEMICONDUCTOR PHOTOCATALYST AND PREPARATION METHOD THEREOF

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

MONOMETALLIC RHODIUM-CONTAINING FOUR-WAY CONVERSION CATALYSTS FOR GASOLINE ENGINE EMISSIONS TREATMENT SYSTEMS

Catalyzed particulate filters comprise three-way conversion (TWC) catalytic material, which comprises rhodium as the only platinum group metal, that permeates walls of a particulate filter. Such catalyzed particulate filters may be located downstream of close-coupled three-way conversion (TWC) composites in an emission treatment system downstream of a gasoline direct injection engine for treatment of an exhaust stream comprising hydrocarbons, carbon monoxide, nitrogen oxides, and particulates. 1. An emission treatment system downstream of a gasoline direct injection engine for treatment of an exhaust stream comprising hydrocarbons , carbon monoxide , nitrogen oxides , and particulates , the emission treatment system comprising:a close-coupled three-way conversion (TWC) composite comprising a first TWC catalytic material on a flow-through substrate; andan catalyzed particulate filter located downstream of the close-coupled TWC composite, the catalyzed particulate filter comprising a second TWC catalytic material that permeates walls of a particulate filter,wherein the second TWC catalytic material comprises rhodium as the only platinum group metal.2. The emission treatment system of claim 1 , wherein the particulate filter comprises a mean pore diameter of about 13 to about 25 μm.3. The emission treatment system of claim 1 , wherein:the particulate filter has a wall thickness of about 6 mils (152 μm) to about 14 mils (356 μm) and an uncoated porosity in the range of 55 to 70%, and,the uncoated porosity is a percentage of volume of pores of the particulate filter relative to volume of the particulate filter.4. The emission treatment system of claim 1 , wherein the catalyzed particulate filter has a coated porosity that is less than an uncoated porosity of the particulate filter.5. The emission treatment system of claim 4 , wherein there is no layering of catalytic material on the surface of the walls of the particulate filter except optionally in areas of overlapped ...

Na-Y Molecular Sieve, H-Y Molecular Sieve, and Preparation Methods Thereof, Hydrocracking Catalyst, and Hydrocracking Method

Provided is a Na—Y molecular sieve and a method for preparing the Na—Y molecular sieve, an H—Y molecular sieve and a method for preparing the H—Y molecular sieve, a hydrocracking catalyst, and a hydrocracking method. The average grain diameter of the Na—Y molecular sieve is 2-5 μm, and the sum of pore volumes of pores in 1-10 nm diameter accounts for 70-90% of the total pore volume of the Na—Y molecular sieve. The H—Y molecular sieve obtained from the large-grain Na—Y molecular sieve can be used as an acidic component in the hydrocracking catalyst. When the hydrocracking catalyst containing the H—Y molecular sieve is applied in the hydrocracking reaction of heavy oils that contain macromolecules, it can provide better cracking activity and product selectivity in the hydrocracking reaction. 1. A hydrocracking catalyst , wherein the support in the catalyst contains an H—Y molecular sieve , wherein the crystal cell parameter of the H—Y molecular sieve is 2.425-2.450 nm; the mole ratio of SiO/AlOin the H—Y molecular sieve is 10-120:1; the sum of pore volumes of pores in 2-7 nm diameter in the H—Y molecular sieve is 60-95% of the total pore volume; the specific surface area of the H—Y molecular sieve is 750-980 m/g; and , the total acid amount measured by near infrared spectroscopy in the H—Y molecular sieve is 0.1-1.0 mmol/g.2. The hydrocracking catalyst according to claim 1 , wherein the crystal cell parameter of the H—Y molecular sieve is 2.436-2.450 nm; the mole ratio of SiO/AlOin the H—Y molecular sieve is 10-50:1; the sum of pore volumes of pores in 2-6 nm diameter in the H—Y molecular sieve is 60-90% of the total pore volume; the specific surface area of the H—Y molecular sieve is 750-950 m/g; and claim 1 , the total acid amount measured by near infrared spectroscopy in the H—Y molecular sieve is 0.5-1.0 mmol/g.3. The hydrocracking catalyst according to claim 1 , wherein the crystal cell parameter of the H—Y molecular sieve is 2.425-2.435 nm; the mole ratio of SiO ...

Method for producing transition alumina catalyst monoliths

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

ULTRA-STABLE HEAVY HYDROCARBON HYDROPROCESSING CATALYST AND METHODS OF MAKING AND USE THEREOF

An ultra-stable catalyst composition for hydroprocessing hydrocarbon feedstocks and a method of making and use of the ultra-stable catalyst composition. The catalyst composition of the invention comprises a calcined mixture made by calcining a formed particle of a mixture comprising an inorganic oxide material, molybdenum trioxide, and a nickel compound; wherein the calcined mixture is further overlaid with a cobalt component and a molybdenum component to thereby provide the catalyst composition. 1. A catalyst , comprising: a calcined mixture made by calcining a formed particle of a mixture comprising an inorganic oxide material , molybdenum trioxide , and a nickel compound; wherein said calcined mixture is further overlaid with a cobalt component and a molybdenum component to thereby provide said catalyst.2. A catalyst as recited in claim 1 , wherein said mixture further comprises a phosphorus compound.3. A catalyst as recited in claim 2 , wherein the phosphorus content of said catalyst is in the range of from 0.5 wt. % to 4 wt. % of the total weight of said catalyst with the phosphorus content of said calcined mixture being in the range of from 0.05 wt. % to 2 wt. % of the total weight of said calcined mixture.4. A catalyst as recited in claim 3 , wherein said calcined mixture is additionally overlaid with a phosphorus component.5. A catalyst as recited in claim 4 , wherein the phosphorus content of said catalyst is in the range of from 0.5 wt. % to 4 wt. % of the total weight of said catalyst with the phosphorus content of said calcined mixture being in the range of from 0.05 wt. % to 2 wt. % of the total weight of said calcined mixture.6. A catalyst as recited in claim 1 , wherein the molybdenum content of said calcined mixture is in the range of from 2 wt. % to 10 wt. % of the total weight of said calcined mixture claim 1 , and the nickel content of said calcined mixture is in the range of from about 0.5 wt. % to about 4 wt. % of the total weight of said ...

SELF-ACTIVATING HYDROPROCESSING CATALYST HAVING ENHANCED ACTIVITY AND SELF-ACTIVATION CHARACTERISTICS AND ITS USEFOR TREATING RESID FEEDSTOCKS

A self-activating catalyst for treating heavy hydrocarbon feedstocks that comprises a calcined particle treated with a sulfoxide compound in the presence of hydrogen. The calcined particle comprises a co-mulled mixture made by co-mulling inorganic oxide powder, molybdenum trioxide powder, and a nickel compound and then forming the co-mulled mixture into a particle that is calcined to thereby provide the calcined particle. The calcined particle comprises from 1 to 10 weight percent molybdenum and nickel that is present in an amount such that the weight ratio of said nickel-to-molybdenum is less than 0.4. The calcined particle has a pore size distribution that contributes to the unique properties of the catalyst. The enhanced self-activating catalyst is used in the hydroprocessing of heavy residue feedstocks that have high nickel, vanadium and sulfur concentrations. 1. A self-activating hydroprocessing catalyst for treating heavy hydrocarbon feedstocks , wherein said catalyst comprises:a calcined particle treated with a sulfoxide compound in the presence of hydrogen, wherein said calcined particle comprises a co-mulled mixture made by co-mulling inorganic oxide powder, molybdenum trioxide powder, and a nickel compound that is formed into a particle of said co-mulled mixture that is thereafter calcined;wherein said calcined particle comprises molybdenum in an amount from 1 to 10 weight percent, nickel in an amount such that the weight ratio of nickel-to-molybdenum is less than 0.4; andwherein said weight percents are for the metal and on the basis of the total weight of the calcined particle.2. A self-activating hydroprocessing catalyst as recited in claim 1 , wherein the treatment of said calcined particle is conducted by contacting said calcined particle with a petroleum-derived hydrocarbon feedstock claim 1 , having a concentration of said sulfoxide compound such that the sulfur content of said petroleum-derived hydrocarbon feedstock contributed by said sulfoxide ...

POROUS STRUCTURE FOR EXHAUST GAS PURIFICATION CATALYST, EXHAUST GAS PURIFICATION CATALYST USING POROUS STRUCTURE, AND EXHAUST GAS PURIFICATION METHOD

Provided is a porous structure for exhaust purification catalysts having excellent light-off temperature characteristics. The porous structure for exhaust purification catalysts includes an oxygen storage component and an inorganic porous solid. The porous structure has a pore volume distribution such that the ratio of the pore volume of pores with a diameter of from 15 nm to less than 25 nm to the pore volume of pores with a diameter of from 5 nm to less than 15 nm is 1.3 to 2.5 as measured with a mercury porosimeter. The pore volume distribution preferably has at least one peak top in a pore diameter range of from 15 nm to less than 25 nm. 110-. (canceled)11. An exhaust gas purification catalyst comprising a substrate and a catalyst layer on the substrate ,the catalyst layer comprising an oxygen storage component and an inorganic porous solid,the exhaust gas purification catalyst having a pore volume distribution such that a ratio of a pore volume of pores with a diameter of from 15 nm to less than 25 nm to a pore volume of pores with a diameter of from 5 nm to less than 15 nm is 1.4 to 2.5 as measured with a mercury porosimeter,the pore volume distribution having at least one peak top in a pore diameter range of from 15 nm to less than 25 nm, andthe pore volume distribution having a ratio of a pore volume of pores with a diameter of from 5 nm to less than 15 nm to a pore volume of pores with a diameter of 5 to 200 nm is 15% to 35%, and a ratio of a pore volume of pores with a diameter of from 15 nm to less than 25 nm to a pore volume of pores with a diameter of 5 to 200 nm is 25% to 55%.12. The exhaust gas purification catalyst according to claim 11 , wherein the pore volume distribution has a ratio of a pore volume of pores with a diameter of from 5 nm to less than 15 nm to the total pore volume is 5% to 35% claim 11 , and a ratio of a pore volume of pores with a diameter of 15 nm to less than 25 nm to the total pore volume is 10% to 50%.13. The exhaust gas ...

CATALYTIC MODULE WITH IMPROVED EFFECTIVENESS IN TERMS OF AGEING

A catalytic module, containing a solid support, and a stack including at least the following layers arranged in the following order, taking the solid support as a base: 1. A catalytic module , comprising:a solid support; anda stack comprising at least the following layers arranged in the following order, starting from the solid support:{'sub': '2', 'a first porous layer comprising CeOand deposited by chemical vapour deposition, and'}a first catalytic layer comprising at least one metal and/or at least one alloy of metals selected from the group consisting of Pt, Pd, and Rh, said first catalytic layer being deposited by chemical vapour deposition.2. The catalytic module according to claim 1 , wherein the first layer comprising CeOis discontinuous and comprises islands.3. The catalytic module according to claim 1 , comprising a second porous layer comprising CeOformed on the first catalytic layer.4. The catalytic module according to claim 3 , comprising a second catalytic layer formed on the second porous layer comprising CeO.5. The catalytic module according to claim 1 , comprising a buffer layer between the solid support and the first porous layer comprising CeO claim 1 , said buffer layer comprising at least one metal oxide6. The catalytic module according to claim 5 , wherein the buffer layer comprises one or several mixed oxides of different natures.7. The catalytic module according to claim 1 , wherein the first porous layer comprising CeOforms a buffer layer.8. The catalytic module according to claim 1 , wherein the first and/or the second porous layer comprising CeOcomprises mainly CeO.9. The catalytic module according to claim 1 , wherein the first and/or the second porous layer comprising CeOfurther comprises zirconia.10. The catalytic module according to claim 1 , wherein the first and/or the second porous layer comprising CeOfurther comprises yttriated zirconia.11. The catalytic module according to claim 1 , wherein the solid support is a macroporous ...

PREPARATION OF A ZSM-5-BASED CATALYST; USE IN ETHYLBENZENE DEALKYLATION PROCESS

A process of preparing a catalyst composition which process comprises the steps of (a) treating ZSM-5 zeolite with an alkaline solution having a pH of at least (8) followed by ion exchange to obtain a treated zeolite, (b) extruding a mixture of the treated zeolite and binder and contacting the zeolite with a fluorocompound containing solution, (c) increasing the temperature of the extrudates obtained in step (b) to at least 200° C., and (d) combining the extrudates obtained in step (c) with one or more metals selected from the group consisting of Group (10) and (11) of the IUPAC Periodic Table of Elements and a process for the conversion of an aromatic hydrocarbons containing feedstock using a catalyst composition prepared by such process. 1. A process of preparing a catalyst composition which process comprises the steps of:(a) treating ZSM-5 zeolite with an alkaline solution having a pH of at least 8 followed by ion exchange to obtain a treated zeolite,(b) extruding a mixture of the treated zeolite and a binder and contacting the zeolite with a fluorocompound containing solution,(c) increasing the temperature of the extrudates obtained in step (b) to at least 200° C., and(d) combining the extrudates obtained in step (c) with one or more metals selected from the group consisting of Group 10 and 11 of the IUPAC Periodic Table of Elements.2. The process according to in which step (b) comprises extruding a mixture of the treated zeolite and silica binder claim 1 , and subsequently treating the extrudates with a fluorocompound containing solution.3. The process according to in which step (b) comprises treating the extrudates with a solution comprising a fluorosilicate.4. The process according to in which the metal is selected from the group consisting of platinum and palladium.5. The process according to in which the extrudate is further combined with one or more metal chosen from the group consisting of tin and rhenium.6. The process according to in which the ZSM-5 ...

FUNGICIDE, PHOTO CATALYTIC COMPOSITE MATERIAL, ADSORBENT, AND DEPURATIVE

Disclosed herein is a fungicide, including: a porous carbon material; and a silver member adhered to the porous carbon material, wherein a value of a specific surface area based on a nitrogen BET, namely 1. A photo catalytic composite material comprising:a porous carbon material; anda photo catalytic material adhered to said porous carbon material,{'sup': 2', '3, 'wherein a value of a specific surface area based at least in part on a nitrogen BET method is greater than or equal to 10 m/g, and a volume of a fine pore based at least in part on a BJH method and an MP method is greater than or equal to 0.1 cm/g.'}2. The photo catalytic composite material according to claim 1 , wherein said photo catalytic material absorbs an energy of a light having a wavelength between 200 to 600 nm.3. The photo catalytic composite material according to claim 1 , further comprising a titanium oxide doped either with a cation or with an anion.4. The photo catalytic composite material according to claim 3 , wherein the cation includes at least one of a chromium ion claim 3 , an iron ion claim 3 , a silver ion claim 3 , a platinum ion claim 3 , a copper ion claim 3 , a tungsten ion claim 3 , or claim 3 , a cobalt ion and a nickel ion.5. The photo catalytic composite material according to claim 1 , wherein silicon oxide is removed away from the porous carbon material.6. The photo catalytic composite material according to claim 1 , wherein the porous carbon material has a distribution of fine pores with a peak in a range of 3 to 20 nm.7. The photo catalytic composite material according to claim 1 , wherein the porous carbon material includes silicon.8. A depurative obtained from the photo catalytic composite material according to .9. A depurative claim 1 , comprising:a porous carbon material; andan organic material adhered to said porous carbon material,{'sup': 2', '3, 'wherein a value of a specific surface area based on a nitrogen BET method is equal to or greater than 10 m/g, and a volume ...

CO-MIXED CATALYST PRODUCED FROM SOLUTIONS CONTAINING HETEROPOLYANIONS, METHOD FOR THE PRODUCTION THEREOF, AND USE OF SAME IN HYDROCONVERSION OF HEAVY HYDROCARBON FEEDSTOCK

The present invention relates to a process for the preparation of catalyst(s), comprising the cokneading of boehmite with an active phase comprising a salt of heteropolyanion of Keggin and/or lacunary Keggin and/or substituted lacunary Keggin and/or Anderson and/or Strandberg type, and their mixtures, exhibiting, in its structure, molybdenum and cobalt and/or nickel. The present invention also relates to a process for the hydrotreating and/or hydroconversion of a heavy hydrocarbon feedstock in the presence of catalyst(s) prepared according to said process. 1. A process for the preparation of a catalyst comprising an active phase comprising molybdenum and nickel and/or cobalt , and an oxide matrix predominantly composed of alumina , said catalyst comprising a total pore volume of at least 0.6 ml/g , a macropore volume of between 10.0% and 40.0% of the total pore volume , a mesopore volume of at least 0.5 ml/g and a mean mesopore diameter of greater than 5.0 nm , comprising the following stages:a) a stage of preparation of an aqueous solution of aluminum precursors comprising a first acidic aluminum precursor, chosen from aluminum sulfate, aluminum chloride, aluminum nitrate and their mixtures, and a first basic aluminum precursor, chosen from sodium aluminate, potassium aluminate, ammonia, sodium hydroxide, potassium hydroxide and their mixtures;b) a stage of bringing the solution obtained on conclusion of stage a) into contact with a second basic precursor, chosen from sodium aluminate, potassium aluminate, ammonia, sodium hydroxide, potassium hydroxide and their mixtures, and with a second acidic precursor chosen from aluminum sulfate, aluminum chloride, aluminum nitrate, sulfuric acid, hydrochloric acid, nitric acid and their mixtures, in order to obtain a suspension, with at least one of the second basic or acidic precursors comprising aluminum, the relative flow rate of the second acidic and basic precursors being chosen so as to obtain a pH of the reaction ...

Aromatization Processes Using Both Fresh and Regenerated Catalysts, and Related Multi-Reactor Systems

Multi-reactor systems with aromatization reactor vessels containing a catalyst with low surface area and pore volume, followed in series by aromatization reactor vessels containing a catalyst with high surface area and pore volume, are disclosed. Related reforming methods using the different aromatization catalysts also are described. 111-. (canceled)12. An aromatization reactor vessel system comprising:(A) at least one first reactor vessel comprising:(a1) a first reactor inlet for introducing a first hydrocarbon feed into the at least one first reactor vessel;(a2) a first aromatization catalyst for catalytically converting at least a portion of the first hydrocarbon feed under first reforming conditions to produce a first aromatic product; wherein the first aromatization catalyst comprises a first transition metal and a first catalyst support, the first aromatization catalyst characterized by:{'sup': 2', '2, 'a first surface area in a range from about 80 m/g to about 150 m/g; and/or'}a first micropore volume in a range from about 0.01 cc/g to about 0.048 cc/g; and(a3) a first reactor outlet for discharging a first effluent comprising the first aromatic product from the at least one first reactor vessel;(B) at least one second reactor vessel comprising:(b1) a second reactor inlet for introducing a second hydrocarbon feed into the at least one second reactor vessel;(b2) a second aromatization catalyst for catalytically converting at least a portion of the second hydrocarbon feed under second reforming conditions to produce a second aromatic product; wherein the second aromatization catalyst comprises a second transition metal and a second catalyst support, the second aromatization catalyst characterized by:{'sup': 2', '2, 'a second surface area in a range from about 160 m/g to about 260 m/g; and/or'}a second micropore volume in a range from about 0.05 cc/g to about 0.09 cc/g; and(b3) a second reactor outlet for discharging a second effluent comprising the second ...

METHOD OF PREPARING AN ACTIVATED EU-2 ZEOLITE

Disclosed herein is a method of making activated EU-2 zeolite, including: pores having a diameter of 30 to 40 Å while maintaining the crystal structure of the EU-2 zeolite; and pores having a diameter of 40 to 200 Å, wherein the volume of the pores having a diameter of 30 to 40 Å is 0.01 to 0.06 cc/g, and the volume of the pores having a diameter of 40 to 200 Å is 0.07 to 0.4 cc/g. 1. A method of preparing an activated EU-2 zeolite , comprising the steps of:a) hydrothermally synthesizing an EU-2 zeolite; andb) activating the EU-2 zeolite by bringing the EU-2 zeolite into contact with an aqueous alkali solution before or after calcining the EU-2 zeolite,wherein the activated EU-2 zeolite comprises:pores having a diameter of 30 to 40 Å while maintaining a crystal structure of the EU-2 zeolite; andpores having a diameter of 40 to 200 Å,wherein a volume of the pores having a diameter of 30 to 40 Å is 0.01 to 0.06 cc/g, and a volume of the pores having a diameter of 40 to 200 Å is 0.07 to 0.4 cc/g.2. The method of claim 1 , wherein claim 1 , in the step b) claim 1 , a molar ratio of alkali cation to aluminum (Na/AlO) in the EU-2 zeolite is 0.1 to 0.3.3. The method of claim 1 , further comprising the step of: c) substituting alkali cation in the activated EU-2 zeolite with ammonium ion.4. The method of claim 1 , wherein claim 1 , in the step b) claim 1 , a molar ratio of silica/alumina in the activated EU-2 zeolite is reduced by 6 to 59% compared to the EU-2 zeolite before the step b).5. The method of claim 1 , wherein claim 1 , in the step a) claim 1 , a molar ratio of silica/alumina in the hydrothermally synthesized EU-2 is 80 to 300.6. The method of claim 1 , wherein claim 1 , in the step a) claim 1 , a volume of the pores having a diameter of 30 to 40 Å in the hydrothermally synthesized EU-2 zeolite is 0.01 to 0.05 cc/g claim 1 , and a volume of the pores having a diameter of 40 to 200 Å therein is 0.05 cc/g or less.7. The method of claim 1 , wherein claim 1 , in the ...

Process for Preparing a Molecular Sieve

The present invention provides a mordenite zeolite having a mesopore surface area of greater than 30 m/g and an average primary crystal size as measured by TEM of less than 80 nm, and methods of making the mordenite zeolite. 114.-. (canceled)15. A process for converting a feedstock comprising an organic compound to a conversion product which comprises the step of contacting said feedstock at organic compound conversion conditions with a catalyst comprising a mordenite zeolite , the mordenite zeolite comprising a structure directing agent (SDA) selected from the group consisting of TEA , MTEA and mixtures thereof within its pores , having a mesopore surface area of greater than 30 m/g and comprising agglomerates composed of primary crystallites , wherein the primary crystallites have an average primary crystal size as measured by TEM of less than 80 nm.16. The process of claim 15 , wherein the primary crystallites have an average primary crystal size of less than 80 nm in each of the a claim 15 , b and c crystal vectors as measured by X-ray diffraction.17. The process of claim 15 , wherein at least 90% by number of the primary crystallites have a primary crystal size of less than 80 nm as measured by TEM.18. The process of claim 15 , wherein said primary crystallites have an aspect ratio of less than 2 claim 15 , wherein the aspect ratio is defined as the longest dimension of the crystallite divided by the width of the crystallite claim 15 , where the width of the crystallite is defined as the dimension of the crystallite in the middle of that longest dimension in a dimension orthogonal to that longest dimension claim 15 , as measured by TEM.19. The process of claim 15 , wherein the mordenite zeolite has a mesopore surface area of greater than 40 m/g.20. The process of claim 15 , wherein the ratio of mesopore surface area to the total surface area is greater than 0.05.21. The process of claim 15 , wherein the mordenite zeolite is a calcined mordenite zeolite prepared ...

Low-Temperature Oxidation Catalyst With Particularly Marked Hydrophobic Properties ForThe Oxidation Of Organic Pollutants

The present invention relates to a catalyst comprising a macroporous noble metal-containing zeolite material and a porous SiO-containing binder, wherein the catalyst has a proportion of micropores of more than 70%, based on the total pore volume of the catalyst. The invention is additionally directed to a process for preparing the catalyst and to the use of the catalyst as an oxidation catalyst. 112-. (canceled)13. A method of purifying exhaust , the method comprising:providing an exhaust gas containing an organic pollutant; a microporous noble metal-containing zeolite material, the zeolite material having less than 2 mol. % aluminium, the zeolite material being selected from zeolites of the types AFI, AEL, BEA, CHA, EUO, FAU, FER, KFI, LTL, MAZ, MOR, MEL, MTW, OFF, TON and MFI, the noble metal being selected from the group consisting of rhodium, iridium, palladium, platinum, ruthenium, osmium, gold and silver and combinations thereof; and', {'sub': '2', 'a porous SiO-containing binder having less than 0.04 wt % aluminium,'}, 'wherein the catalyst has a proportion of micropores having a diameter of less than 1 nm of more than 70% relative to the total pore volume of the catalyst., 'oxidizing the exhaust gas with a catalyst under conditions sufficient to oxidize the organic pollutant, the catalyst comprising'}14. The method according to claim 13 , wherein the exhaust gas is an exhaust gas from a combustion process.15. The method according to claim 13 , wherein the exhaust gas is an exhaust gas from a power plant.16. The method according to claim 13 , wherein the exhaust gas is an exhaust gas from an industrial process.17. The method according to claim 13 , wherein the oxidation is performed at a temperature below 300° C.18. The method according to claim 13 , wherein the organic pollutant is a solvent-type organic pollutant.19. The method according to claim 13 , wherein the organic pollutant is a paraffin claim 13 , an olefin claim 13 , an aldehyde or an aromatic.20. ...

PROCESS FOR PREPARING A MESOPORIZED CATALYST, CATALYST THUS OBTAINED AND USE THEREOF IN A CATALYTIC PROCESS

A hydroconversion catalyst obtained by the process described, comprising a mesoporized zeolite with healed zeolitic structure, containing at least one network of micropores and at least one network of mesopores, having an atomic Si/Al ratio within the zeolite framework of greater than or equal to 2.3 and showing reduced amount of extra-framework aluminium with regard to that of a mesoporized zeolite with no healed zeolitic structure. 3. A process for the hydroconversion of a hydrocarbon feedstock claim 1 , wherein said feedstock to be treated is placed in contact with the hydroconversion catalyst according to . This application is a continuation application of U.S. application Ser. No. 14/347,159, filed on Mar. 25, 2014, which is a National Stage of International Application No. PCT/EP2012/071017 filed Oct. 24, 2012, claiming priority based on French Patent Application No. 11 59618 filed Oct. 24, 2011 and French Patent Application No. 11 62520 filed Dec. 29, 2011, the contents of all of which are incorporated herein by reference in their entirety.The invention relates to a process for preparing a mesopores-containing catalyst, the catalyst thus obtained and the use of the catalyst thus obtained in an industrial process.The catalyst described here comprises a mesoporized zeolite and may be used in many hydroconversion processes, in particular, in the hydrocracking process.The various zeolites are distinguished by different structures and properties, and are well known in the art. A few structures commonly used in the field of catalysis are disclosed in WO2010/072976, among them some are given below.Zeolite Y (FAU) is a three-dimensional zeolite with large pores, whose structure has large cavities interconnected by channels formed from 12-membered rings, each ring presenting 12 (Si and Al) cations and 12 O anions.Beta zeolite (BEA) is a three-dimensional zeolite with large pores comprising pores formed from 12-membered rings in all directions.Zeolite ZMS-5 (MFI) is a ...

MESOPOROUS METAL TITANATES AS MULTIFUNCTIONAL CATALYSTS

The present disclosure relates to mesoporous metal titanate materials composition. Specifically, the present disclosure relates to a mesoporous metal titanate material composition that is active for multiple reactions, including aromatic alkylation, alkene coupling, alkene cyclization, alkyne oxidation, alcohol dehydrogenation reactions. 1. A mesoporous metal titanate material.2. The mesoporous metal titanate material according to claim 1 , wherein the material has an average pore diameter from about 2 to about 7 nm.3. The mesoporous metal titanate material according to claim 1 , wherein the material has a surface area of about 200 m/g to about 550 m/g.4. The mesoporous metal titanate material according to claim 1 , wherein the material is in the form of one or more particles.5. The mesoporous metal titanate material according to claim 1 , wherein the one or more particles have an average particle diameter of less than 50 nm.6. The mesoporous metal titanate material according to claim 1 , wherein the material has a monomodal pore size distribution.7. The mesoporous metal titanate material according to claim 1 , wherein the material has a homogenous pore size distribution throughout the material.8. The mesoporous metal titanate material according to claim 1 , wherein the metal is a transition metal claim 1 , a p-block metal claim 1 , an s-block metal claim 1 , or a lanthanide.9. The mesoporous metal titanate material according to claim 8 , wherein the metal is a transition metal.10. The mesoporous metal titanate material according to claim 9 , wherein the transition metal is a first row-transition metal.11. The mesoporous metal titanate material according to claim 8 , wherein the metal is a p-block metal.12. The mesoporous metal titanate material according to claim 8 , wherein the metal is an s-block metal.13. The mesoporous metal titanate material according to claim 8 , wherein the metal is a lanthanide.14. A multifunctional catalyst comprising the mesoporous metal ...

METHOD FOR MAKING HYDRODESULFURIZATION CATALYST INCLUDING CALCINATION

A method of preparing hydrodesulfurization catalysts having cobalt and molybdenum sulfide deposited on a support material containing mesoporous silica. The method utilizes a sulfur-containing silane that dually functions as a silica source and a sulfur precursor. The method involves an one-pot strategy for hydrothermal treatment and a single-step calcination and sulfidation procedure. The application of the hydrodesulfurization catalysts in treating a hydrocarbon feedstock containing sulfur compounds to produce a desulfurized hydrocarbon stream is also specified. 1. A calcination method for making a CoMoS hydrodesulfurization catalyst , the method comprising:mixing a molybdenum precursor, a cobalt precursor, a mercaptoalkyltrialkoxysilane, a structural directing surfactant, an acid, and a solvent to form a reaction mixture;hydrothermally treating the reaction mixture to form a dried mass; andcalcining the dried mass in a reducing atmosphere with an activation gas containing a mixture of hydrogen and an inert gas thereby forming the CoMoS hydrodesulfurization catalyst, wherein the hydrogen is 50-80% by volume relative to a total volume of the reducing atmosphere,wherein:the inert gas is at least one selected from the group consisting of argon, nitrogen, and helium; andthe CoMoS hydrodesulfurization catalyst comprises cobalt and molybdenumsulfide disposed on a support material comprising a mesoporous silica.2. The method of claim 1 , wherein the CoMoS hydrodesulfurization catalyst is not subjected to a sulfidation with a sulfidation reagent.3. The method of claim 1 , wherein the mercaptoalkyltrialkoxysilane is at least one selected from the group consisting of (mercaptomethyl)trimethoxysilane claim 1 , (mercaptomethyl)triethoxysilane claim 1 , (mercaptomethyl)tripropoxysilane claim 1 , (2-mercaptoethyl)trimethoxysilane claim 1 , (2-mercaptoethyl)triethoxysilane claim 1 , (2-mercaptoethyl)tripropoxysilane claim 1 , (3-mercaptopropyl)trimethoxysilane claim 1 , (3- ...

Superficially Porous Hybrid Monoliths with Ordered Pores and Methods of Making and using same

The invention provides superficially porous metal oxide or hybrid metal oxide monoliths with ordered pore structures. The superficially porous hybrid silica monoliths of the invention provide several major advantages over existing silica monoliths. When used in chromatography, the superficially porous hybrid silica monoliths of the invention deliver fast separation at very low back pressure and possess superb pH stability and much improved mechanical strength. 1. A porous monolith , comprising:an organically modified solid skeleton comprising continuous macropores; anda substantially porous outer shell comprising substantially ordered mesopores, wherein both the skeleton and the outer shell are independently metal oxide or hybrid metal oxide; and wherein the metal oxide is selected from silica, alumina, titania and zirconia.2. The porous monolith of claim 1 , wherein the metal oxide is silica.3. The porous monolith of claim 2 , wherein the continuous macropores have a median pore size ranges from about 0.2 μm to about 10 μm.4. The porous monolith of claim 2 , wherein the substantially ordered mesopores have a median pore size ranges from about 1 nm to about 100 nm with a pore size distribution (one standard deviation) of no more than 50% of the median pore size.5. The porous monolith of claim 4 , wherein the substantially ordered mesopores have a median pore size ranges from about 2 nm to about 50 nm with a pore size distribution (one standard deviation) of no more than 50% of the median pore size.6. The porous monolith of claim 2 , wherein the hybrid silica skeletons are modified by silsesquioxane.7. The porous monolith of claim 6 , wherein silsesquioxane comprises bridged polysilsesquioxane.8. The porous monolith of claim 2 , wherein the silica monoliths have a median surface area in the range from about 5 m/g to about 1 claim 2 ,000 m/g.9. The porous monolith of claim 8 , wherein the silica monoliths have a median surface area in the range from about 100 m/g to ...

A solid heterogeneous catalyst for olefin hydroformylation reaction and production method and use thereof

A solid heterogeneous catalyst consisting of a metal component and an organic ligand polymer, wherein the metal component is one or more of Rh, Ir or Co, the organic ligand polymer is a polymer having a large specific surface area and hierarchical porosity formed by polymerizing an organic ligand monomer containing P and alkenyl group and optional N via a solvothermal polymerization process, the metal component forms coordinated bond with the P atom or N in backbone of the organic ligand polymer and exists in a monoatomic dispersion state; when the catalyst is used in an olefin hydroformylation reaction, the metal component and the P and/or N atom form in situ an intermediate active species similar to homogeneous catalyst due to the coordination effect, and the catalyst has an excellent catalytic property, can be easily separated, and has a relatively high stability. 1. A solid heterogeneous catalyst for olefin hydroformylation reaction , wherein the solid heterogeneous catalyst consists of a metal component and an organic ligand polymer , wherein the metal component is one or more of Rh , Ir or Co , the organic ligand polymer is a polymer having a large specific surface area and hierarchical porosity formed by polymerizing an organic ligand monomer containing P and alkenyl group and optional N via a solvothermal polymerization process , the metal component forms coordinated bonds with the P atom or N in backbone of the organic ligand polymer and exists in a monoatomic dispersion state.2. The solid heterogeneous catalyst according to claim 1 , wherein the metal component accounts for 0.005 to 5.0% based on the total weight of the solid heterogeneous catalyst.3. The solid heterogeneous catalyst according to claim 1 , wherein the organic ligand monomer is an organic phosphine ligand monomer containing P and vinyl group and optional N.4. The solid heterogeneous catalyst according to claim 1 , wherein the organic ligand polymer has a specific surface area of 100 to 3000 ...

Supported Mixed Oxides Catalysts for Oxidative Coupling of Methane

A supported oxidative coupling of methane (OCM) catalyst comprising a support and an OCM catalytic composition characterized by the general formula A a Z b E c D d O x ; wherein A is an alkaline earth metal; wherein Z is a first rare earth element; wherein E is a second rare earth element; wherein D is a redox agent or a third rare earth element; wherein the first rare earth element, the second rare earth element, and the third rare earth element, when present, are not the same; wherein a is 1.0; wherein b is from about 0.1 to about 10.0; wherein c is from about 0.1 to about 10.0; wherein d is from about 0 to about 10.0; and wherein x balances the oxidation states.

HONEYCOMB STRUCTURE

A honeycomb structure including a honeycomb having porous partition walls extending between inflow and outflow end faces to define cells, an outermost peripheral wall, and a pair of electrodes disposed on a side surface of the honeycomb. Each electrode is formed in a strip shape extending in a direction of the cells. In a cross section orthogonal to the extending direction of the cells, one electrode is disposed on a side opposed to the other electrode. The honeycomb has an outer peripheral region including the outer peripheral wall, a central region, and an intermediate region. An average electric resistivity A of a material constituted of the outer peripheral region, an average electric resistivity B of a material constituted of the central region and an average electric resistivity of C of a material constituted of the intermediate region satisfy the relationship: A≤B Подробнее

CONDUCTIVE HONEYCOMB STRUCTURE

A conductive honeycomb structure that is divided into four equal portions in a flow path direction of cells in the structure to form four regions of A, B, C, and D from a side closer to a first end face, and an average value of electric resistances measured between two points in each of the four regions is represented as R, R, R, and Rin this order from the side closer to the first end face. A relational expression of R≤R≤R≤R(excluding R=R=R=R) is satisfied provided that the two points being determined so that a distance between a pair of electrode layers arranged on an outer peripheral side wall of the structure is the longest in the cross section perpendicular to the flow path direction of the cells. 1. A conductive honeycomb structure , comprising: an outer peripheral side wall; and', 'partition walls disposed inside the outer peripheral side wall defining a plurality of cells to form flow paths so that fluid can enter the flow paths through a first end face and exit through a second end face;, 'a pillar-shaped conductive honeycomb structure portion havingwherein a pair of electrode layers extending in a flow path direction of the cells constitutes a part of an outer surface of the outer peripheral side wall,one electrode layer of the pair of electrode layers is disposed on a side opposite to the other electrode layer across a central axis of the honeycomb structure portion, and{'sub': A', 'B', 'C', 'D', 'A', 'B', 'C', 'D', 'A', 'B', 'C', 'D, 'when the honeycomb structure is divided into four equal portions in the flow path direction of the cells to form four regions of A, B, C, and D from a side closer to the first end face, and an average value of electric resistances measured between two points in each of the four regions is represented as R, R, R, and Rin this order from the side closer to the first end face, a relational expression of R≤R≤R≤R(excluding R=R=R=R) is satisfied provided that the two points being determined so that a distance between the pair of ...

Shaped porous 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.

DUAL CATALYST SYSTEM FOR PROPYLENE PRODUCTION

Embodiments of processes for producing propylene utilize a dual catalyst system comprising a mesoporous silica catalyst impregnated with metal oxide and a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm/g, and the MFI structured silica catalyst has a total acidity of 0.001 mmol/g to 0.1 mmol/g. The propylene is produced from the butene stream via metathesis by contacting the mesoporous silica catalyst and subsequent cracking by contacting the MFI structured silica catalyst. 1. A dual catalyst system for producing propylene from butene , the dual catalyst system comprising a metathesis catalyst zone and a cracking catalyst zone directly downstream of the metathesis catalyst zone where:the metathesis catalyst zone comprises mesoporous silica catalyst impregnated with metal oxide; andthe cracking catalyst zone comprises a mordenite framework inverted (MFI) structured silica catalyst.2. The dual catalyst system of where the metathesis catalyst zone and the cracking catalyst zone are disposed in one reactor.3. The dual catalyst system of in which at least a portion of the MFI structured silica catalyst is in contact with at least a portion of the mesoporous silica catalyst impregnated with metal oxide.4. The dual catalyst system of where the metathesis catalyst zone is disposed in a first reactor and the cracking catalyst zone is disposed in a second reactor directly downstream of the first reactor.5. The dual catalyst system of further comprising a conduit between the first reactor and the second reactor.6. The dual catalyst system of where the metal oxide of the mesoporous silica catalyst comprises one or more oxides of molybdenum claim 1 , rhenium claim 1 , tungsten claim 1 , or combinations thereof.7. The dual catalyst system of where the mesoporous silica catalyst ...

ELECTRICAL RESISTOR, HONEYCOMB STRUCTURE, AND ELECTRIC HEATING CATALYTIC DEVICE

An electrical resistor includes borosilicate particles, Si-containing particles, and pore parts. The pore parts are constituted by gaps between the borosilicate particles and the Si-containing particles and surround the borosilicate particles and the Si-containing particles. A honeycomb structure includes the electrical resistor. An electric heating catalytic device has the honeycomb structure. 1. An electrical resistor comprising:borosilicate particles;Si-containing particles; andpore parts constituted by gaps between the borosilicate particles and the Si-containing particles and surrounding the borosilicate particles and the Si-containing particles whereinthe electrical resistor has a cumulative pore volume of 0.05 ml/g or more.2. The electrical resistor according to claim 1 , wherein{'sup': '−4', 'the electrical resistor has an electrical resistivity of 0.0001 Ω·m or more and 1 Ω·m or less and an electrical resistance increase rate of 0/K or more and 5.0×10/K or less in a temperature range of 25 to 500° C.'}3. The electrical resistor according to claim 1 , whereinthe Si-containing particles are at least one type selected from a group consisting of Si particles, Fe—Si-based particles, Si—W-based particles, Si—C-based particles, Si—Mo-based particles, and Si—Ti-based particles.4. The electrical resistor according to claim 1 , whereinin the borosilicate particles, a content of B atoms is 0.1 mass % or more and 5 mass % or less.5. The electrical resistor according to claim 1 , whereinin the borosilicate particles, a total content of at least one type of alkali atom selected from a group consisting of Na, Mg, K, and Ca is 2 mass % or less.6. The electrical resistor according to claim 1 , whereinthe borosilicate particles are aluminoborosilicate particles.7. The electrical resistor according to claim 1 , whereinthe electrical resistor is configured to be used for a honeycomb structure in an electric heating catalytic device.8. A honeycomb structure comprising{'claim- ...

CATALYST FOR OXIDATIVE DEHYDROGENATION AND METHOD OF PREPARING THE SAME

The present invention relates to a catalyst for oxidative dehydrogenation and a method of preparing the same. More particularly, the present invention provides a catalyst for oxidative dehydrogenation having a porous structure which may easily control heat generation due to high-temperature and high-pressure reaction conditions and side reaction due to the porous structure and thus exhibits superior product selectivity, and a method of preparing the catalyst. 1. A catalyst for oxidative dehydrogenation , comprising a porous aluminum silicate support and a metal oxide having a composition represented by Formula 1 below:{'br': None, 'sub': 2', '4, 'ABO\u2003\u2003[Formula 1]'}wherein A is one or more selected from the group consisting of divalent cation metals and B is one or more selected from the group consisting of trivalent cation metals.2. The catalyst according to claim 1 , wherein A is one or more selected from the group consisting of Cu claim 1 , Ra claim 1 , Ba claim 1 , Sr claim 1 , Ca claim 1 , Be claim 1 , Zn claim 1 , Mg claim 1 , Mn claim 1 , Co claim 1 , and Fe (II).3. The catalyst according to claim 1 , wherein B is one or more selected from the group consisting of Al claim 1 , Fe(III) claim 1 , Cr claim 1 , Ga claim 1 , In claim 1 , Ti claim 1 , La claim 1 , and Ce.4. The catalyst according to claim 1 , wherein the aluminum silicate of the porous aluminum silicate support is one or more selected from the group consisting of metal oxides claim 1 , metal carbides claim 1 , metal nitrides claim 1 , and hydrated aluminum silicates.5. The catalyst according to claim 1 , wherein the aluminum silicate of the porous aluminum silicate support is a kaolin-based mineral.6. The catalyst according to claim 1 , wherein the porous aluminum silicate support has a pore distribution of 1 to 500 ppi (pores per inch).7. The catalyst according to claim 1 , wherein the metal oxide is comprised in an amount of 1 to 50% by weight based on the catalyst for oxidative ...

SHAPED POROUS 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. 1146-. (canceled)147. A process for the selective oxidation of an aldose to an aldaric acid comprising reacting the aldose with oxygen in the presence of a catalyst composition to form the aldaric acid , wherein the catalyst composition comprises a shaped porous carbon product as a catalyst support and a catalytically active component , wherein the shaped porous carbon product comprises:(a) carbon black and{'sup': 2', '2', '3, '(b) a carbonized binder comprising a carbonization product of a water soluble organic binder and wherein the shaped porous carbon product has a BET specific surface area from about 20 m/g to about 500 m/g, a mean pore diameter greater than about 5 nm, a specific pore volume greater than about 0.1 cm/g, a carbon black content of at least about 35 wt. %, and a carbonized binder content from about 20 wt. % to about 50 wt. %.'}148160-. (canceled)161. The process of claim 147 , wherein the aldose comprises a pentose and/or a hexose.162. The process of claim 161 , wherein the pentose comprises ribose claim 161 , arabinose claim 161 , xylose claim 161 , and/or lyxose.163. The process of claim 161 , wherein the hexose comprises glucose claim 161 , allose claim 161 , altrose claim 161 , mannose claim 161 , gulose claim 161 , idose claim 161 , galactose claim 161 , and/or talose.164. The process of claim 147 , wherein the aldaric acid is selected from the group consisting of xylaric acid and glucaric acid.165. The process of claim 147 , wherein the aldaric acid comprises glucaric acid.166. The process of claim 147 , wherein the catalytically ...

FCC CATALYST WITH ENHANCED MESOPOROSITY, ITS PREPARATION AND USE

Process for the preparation of a catalyst and a catalyst comprising enhanced mesoporosity is provided herein. Thus, in one embodiment, provided is a particulate FCC catalyst comprising 2 to 50 wt % of one or more ultra stabilized high Si02/A1203 ratio large pore faujasite zeolite or a rare earth containing USY, 0 to 50 wt % of one or more rare-earth exchanged large pore faujasite zeolite, 0 to 30 wt % of small to medium pore size zeolites, 5 to 45 wt % quasi-crystalline boehmite 0 to 35 wt % microcrystalline boehmite, 0 to 25 wt % of a first silica, 2 to 30 wt % of a second silica, 0.1 to 10 wt % one or more rare earth components showiomg enhanced mesoporosity in the range of 6-40 nm, the numbering of the silica corresponding to their orders of introduction in the preparation process. 1. An FCC catalyst composition comprising a first zeolite of about 2 to about 50 wt % selected from the group of one or more ultra stabilized or rare earth exchanged ultra stabilized high SiO2/Al2O3 ratio Y , optionally a second zeolite of 0 to about 50 wt % of one or more rare-earth exchanged Y zeolite , optionally 0 to 30 wt % of small to medium pore zeolite , about 5 to about 45 wt % quasicrystalline boehmite , about 0 to about 35 wt % microcrystalline boehmite , a first silica of about 0 to about 20 wt % , a second silica of about 2 to about 30 wt % , about 0.1 to about 10 wt % one or more rare earth components as oxide and the balance clay.2. The FCC Catalyst of wherein the catalyst has increased mesopores in the range of 6-40 nm compared to standard base catalysts.3. The FCC Catalyst of further comprising a pore diameter distribution having a peak at a pore diameter of about 2.0 to about 6 nm.4. The FCC Catalyst of has about 20 to about 30% of the total pore volume contributed by pores at a diameter of about 2.0 to about 6 nm and about 55 to about 70% of the pore volume of pores at a diameter of about 6 to 40 nm.5. The FCC Catalyst of wherein the first zeolite is one or more ...

SHAPED POROUS 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. 1160-. (canceled)161. A process for the hydrogenolysis of glycerol comprising feeding a feed composition comprising glycerol to a reaction zone and reacting the glycerol with hydrogen in the presence of a catalyst composition of in the reaction zone to form a reaction product comprising propylene glycol and/or ethylene glycol , wherein the catalyst composition comprises a shaped porous carbon product as a catalyst support and a catalytically active component or precursor thereof , wherein the shaped porous carbon product comprises:(a) carbon black and{'sup': 2', '2', '3, '(b) a carbonized binder comprising a carbonization product of a water soluble organic binder and wherein the shaped porous carbon product has a BET specific surface area from about 20 m/g to about 500 m/g, a mean pore diameter greater than about 5 nm, a specific pore volume greater than about 0.1 cm/g, a carbon black content of at least about 35 wt. %, and a carbonized binder content from about 20 wt. % to about 50 wt. %, and'}wherein the shaped porous carbon product has a radial piece crush strength greater than about 4.4 N/mm (1 lb/mm) and/or a mechanical piece crush strength greater than about 22 N (5 lbs).162. A process for the hydrogenolysis of glycerol comprising feeding a feed composition comprising glycerol to a reaction zone and reacting the glycerol with hydrogen in the presence of a catalyst composition in the reaction zone to form a reaction product comprising propylene glycol and/or ethylene glycol , wherein the catalyst composition comprises a catalytically active component ...

COPPER SUPPORTED CATALYST COMPRISING A CA-DEFICIENT HYDROXYAPATITE FOR WASTE GAS NOX REMOVAL

A porous material comprises at least 60 wt % of a calcium-deficient hydroxyapatite having a Ca/P molar ratio of less than 1.67, having a specific BET surface area of at least 110 m/g and a pore volume of at least 0.41 cm/g, both measured after heat treatment at 120° C. A catalyst composition for catalytic reduction of NOcompounds, comprising an active catalyst component: Cu and/or CuO deposited on the porous material as support. A deNOx process according to which an ammonia source is injected into a combustion waste gas stream containing NOx; and to which the catalyst composition is brought into contact with the waste gas stream at a temperature of at least 100° C. and preferably at most 600° C. to carry out, in the presence of O, a reduction by NHof at least a portion of the NOx. 1- A porous material or support comprising at least 60 wt % of a calcium-deficient hydroxyapatite having a calcium to phosphate molar ratio (Ca/P) of less than 1.67 ,{'sup': 2', '3, 'said porous support having a specific BET surface area of at least 110 m/g and a pore volume of at least 0.41 cm/g, both measured after heat treatment at 120° C.'}2- The porous material or support according to claim 1 , further comprising calcium carbonate in an amount of less than 20 wt % and more than 0 wt %.3- The porous material or support according to claim 1 , comprising less than 1 wt % of calcium dihydroxide Ca(OH).4- The porous material or support according to claim 1 , further comprising water in an amount of less than 20 wt % and more than 0 wt %.5- The porous material or support according to claim 1 , comprising a Ca/P molar ratio of 1.60 or more.6- The porous material or support according to claim 1 , comprising a Ca/P molar ratio greater than the Ca/P molar ratio of the calcium-deficient hydroxyapatite.7- The porous material or support according to claim 1 , comprisingat least 65 wt % of the calcium-deficient hydroxyapatite, 'at most 99 wt % of the calcium-deficient hydroxyapatite.', 'and/or ...

MACROPOROUS OXYGEN CARRIER SOLID WITH A REFRACTORY FELDSPAR/FELDSPATHOID, METHOD FOR THE PREPARATION THEREOF, AND USE THEREOF IN A CHEMICAL-LOOPING OXIDATION-REDUCTION METHOD

The invention relates to an oxygen carrier solid, its preparation and its use in a method of combustion of a hydrocarbon feedstock by active mass chemical-looping oxidation-reduction, i.e. chemical-looping combustion (CLC). The solid, which is hi the form of particles, comprises an oxidation-reduction active mass composed of metal oxide(s) dispersed in a ceramic matrix comprising at least at least one feldspar or feldspathoid with a melting point higher than 1500° C., such as celsian, and has, initially, a specific macroporous texture. The oxygen carrier solid is prepared from a precursor of the ceramic matrix, obtained from a macroporous zeolitic material with zeolite crystals of a specific size, and a precursor of the oxidation-reduction active mass. 1. An oxygen carrier solid in the form of particles for a process for chemical looping redox combustion of a hydrocarbon feedstock , comprising:a redox active mass constituting between 5% and 75% by weight of the oxygen carrier solid, the redox active mass comprising a metal oxide or a mixture of metal oxides and being capable of transporting oxygen in the chemical looping redox combustion process;a ceramic matrix within which the redox active mass is dispersed, the ceramic matrix constituting between 25% and 95% by weight of the oxygen carrier solid, and the ceramic matrix comprising between 60% and 100% by weight of at least one feldspar or feldspathoid having a melting point above 1500° C. and between 0% and 40% of at least one oxide;a porosity such that:the total pore volume of the oxygen carrier solid, measured by mercury porosimetry, is between 0.05 and 0.9 ml/g,the pore volume of the macropores constitutes at least 10% of the total pore volume of the oxygen carrier solid;the size distribution of the macropores within the oxygen carrier solid, measured by mercury porosimetry, is between 50 nm and 7 μm.2. The oxygen carrier solid as claimed in claim 1 , wherein the total pore volume of the oxygen carrier solid is ...

METHOD FOR PRODUCING A PELLET, PELLET, CATALYST CHARGE, AND STATIC MIXER

The invention relates to a method for producing a pellet, in particular for a catalytic convertor and/or static mixer. The method comprises a trimming and/or deforming of at least one layer of metal foam material into a pellet shape. 115.-. (canceled)16. A method of producing a pellet , comprising the method steps: cutting to shape and/or shaping at least one layer of metal foam material into a pellet shape.17. The method in accordance with claim 16 , wherein the pellet is a pellet for a catalyst and/or for a static mixer.18. The method in accordance with claim 16 , wherein the metal foam material is sintered.19. The method in accordance with claim 16 , wherein the metal foam material has pores having diameters that are distributed in one of a monomodal and a multimodal manner.20. The method in accordance with claim 16 , wherein the metal foam material has pores having diameters that are distributed in a bimodal manner.21. The method in accordance with claim 16 , wherein at least two layers of different metal foam material are provided.22. The method in accordance with claim 21 , wherein said at least two layers of different metal foam material are connected to one another by pressing and/or soldering by means of a soldering film.23. The method in accordance with claim 16 , wherein the pellet has a volume of 0.5 mm3 to 30 cm3.24. The method in accordance with claim 16 , wherein the metal foam material includes pores that have a diameter of 10 μm to 10 claim 16 ,000 μm.25. A pellet comprising at least one layer of metal foam.26. The pellet in accordance with claim 25 , further comprising at least one outer-side indentation and/or groove and/or at least one winding and/or twist of a layer of metal foam.27. The pellet in accordance with claim 25 , wherein at least one outer surface and/or one inner boundary surface of the pellet is at least partly closed.28. The pellet in accordance with claim 25 , wherein the pellet comprises at least two layers of different metal ...

MACROPOROUS OXYGEN CARRIER SOLID WITH AN OXIDE CERAMIC MATRIX, METHOD FOR THE PREPARATION THEREOF, AND USE THEREOF FOR A CHEMICAL-LOOPING OXIDATION-REDUCTION METHOD

The invention relates to an oxygen carrier solid, its preparation and its use in a method of combustion of a hydrocarbon feedstock by active mass chemical-looping oxidation-reduction, i.e. chemical-looping combustion (CLC). The solid, which is in the form of particles, comprises an oxidation-reduction active mass composed of metal oxide(s) dispersed in a ceramic matrix comprising at least one oxide with a melting point higher than 1500° C., such as alumina, and has, initially, a specific macroporous texture. The oxygen carrier solid is prepared from an aqueous suspension containing precursor oxide grains for the ceramic matrix that have a specific size, by a spray-drying technique. 1. An oxygen carrier solid in the form of particles for a process for chemical looping redox combustion of a hydrocarbon feedstock , comprising:a redox active mass constituting between 5% and 75% by weight of the oxygen carrier solid, the redox active mass comprising a metal oxide or a mixture of metal oxides and being capable of transporting oxygen in the chemical looping redox combustion process;a ceramic matrix within which the redox active mass is dispersed, the ceramic matrix constituting between 25% and 95% by weight of the oxygen carrier solid, the said ceramic matrix comprising 100% by weight of at least one oxide having a melting point above 1500° C.; the total pore volume of the oxygen carrier solid, measured by mercury porosimetry, is between 0.05 and 1.2 ml/g,', 'the pore volume of the macropores constitutes at least 10% of the total pore volume of the oxygen carrier solid;', 'the size distribution of the macropores within the oxygen carrier solid, measured by mercury porosimetry, is between 50 nm and 7 μm., 'a porosity such that2. The oxygen carrier solid as claimed in claim 1 , wherein the total pore volume of the oxygen carrier solid is between 0.1 and 0.85 ml/g.3. The oxygen carrier solid as claimed in claim 1 , wherein the pore volume of the macropores constitutes at ...

METHOD FOR PRODUCING CATALYSTS OF FORMULA My(Ce1-xLxO2-x/2)1-y FOR THE USE THEREOF IN THE REVERSE WATER-GAS SHIFT REACTION AND PARTIAL OXIDATION OF METHANE INTO SYNTHESIS GAS BY MEANS OF THE METHOD OF COMBUSTION IN SOLUTION

The invention relates to a method for producing catalysts by the method of combustion in solution, to the catalysts produced by said method, and to the particular use thereof in the reverse water-gas shift reaction and in the partial oxidation of the methane into synthesis gas. Therefore, it is understood that the present invention pertains to the area of the green industry aimed at the reduction of COon the planet. 2. The process according to claim 1 , wherein the Ni water soluble salt used in step (a) is Ni(NO).6HO.3. The process according to claim 1 , wherein the Cu water soluble salt used in step (a) is Cu(NO).6HO.4. The process according to claim 1 , wherein the Pt water soluble salt used in step (a) is a salt selected from Tetraammineplatinum (II) Hydroxide Hydrate ((NH)Pt(OH).xHO) and Tetraammineplatinum(II) nitrate (Pt(NH)(NO))5. The process according to any of to claim 1 , wherein the lanthanide is selected from La claim 1 , Pr claim 1 , Nd claim 1 , Sm claim 1 , Eu claim 1 , Gd claim 1 , Tb claim 1 , Dy claim 1 , Ho claim 1 , Er claim 1 , Tm claim 1 , Yb and Lu.6. The process according to claim 5 , characterized in that the lanthanide is Gd.7. The process according to claim 6 , characterized in thatx has a value between 0.05 and 0.2; ory has a value between 0.001 and 0.15.8. The process according to claim 5 , characterized in that the lanthanide is La.9. The process according to claim 8 , characterized in thatx has a value between 0.05 and 0.2; ory has a value between 0.001 and 0.15.10. The process according to claim 5 , characterized in that the lanthanide is Sm.11. The process according to claim 10 , characterized in thatx has a value between 0.05 and 0.2 ory has a value between 0.001 and 0.15.12. The process according to any of to claim 10 , wherein the fuel use in step (a) is selected from glycine claim 10 , urea claim 10 , citric acid and a combination thereof.13. The process according to claim 12 , wherein the fuel use in step (a) is glycine.14. The ...

Compounds and catalysts for the polymerization of olefins

The present invention relates to components of catalysts for the polymerization of olefins comprising a metallocene compound and a magnesium halide which have particular values of porosity and surface area. Group 4 and vanadium metallocenes are useful metallocenes and the components typically include an electron donor such as an ether, ester or ketone. In particular the components of the invention have surface area (BET) greater than about 50 m 2 /g, porosity (BET) greater than about 0.15 cm 3 /g and porosity (Hg) greater than 0.3 cm 3 /g, with the proviso that when the surface area is less than about 150 m 2 g, the porosity (Hg) is less than about 1.5 cm 3 /g. The magnesium halide is complexed by an ether, ester, or ketone electro donor. The components of the invention are particularly suitable for the preparation of catalysts for the gas-phase polymerization of α-olefins.

Catalytically coated support, process for its preparation and thus equipped reactor and its use

Beschrieben werden Träger mit katalytischer Beschichtung, umfassend mindestens eine poröse und Kavitäten enthaltende Katalysatorschicht, wobei die Kavitäten irreguläre Hohlräume mit Abmessungen von größer als 5 mum in mindestens zwei Dimensionen oder mit Querschnittsflächen von mindestens 10 mum·2· darstellen. DOLLAR A Die katalytischen Beschichtungen zeichnen sich durch eine hohe Haftzugfestigkeit aus und lassen sich vorzugsweise in Mikroreaktoren einsetzen. The description relates to supports having a catalytic coating comprising at least one catalyst layer containing porous and cavities, wherein the cavities represent irregular cavities with dimensions of greater than 5 μm in at least two dimensions or with cross-sectional areas of at least 10 μm 2. DOLLAR A The catalytic coatings are characterized by a high adhesive tensile strength and can be used preferably in microreactors.

Honeycomb structure

A honeycomb structure comprising both zeolite and an inorganic binder and having a honeycomb unit in which plural through holes are arranged in the lengthwise direction across a partition wall from each other, wherein the honeycomb unit has a thermal conductivity of 0.15 to 0.60W/m/K and a Young's modulus of 1.5 to 7.0MPa.

Catalyst support, process for its preparation and use

An open-pore catalyst support comprising a material that comprises a natural sheet silicate and ZrO 2 . In order to provide a catalyst support, by means of which alkenyl acetate catalysts can be prepared which are characterized by a high level of alkenyl acetate activity over a relatively long period, the catalyst support comprises a material that comprises a natural sheet silicate and ZrO 2 in the tetragonal modification.

Catalyst based on crystalline aluminosilicate

Catalysts based on pentasil-type crystalline aluminosilicates are of primary crystallites with at least 20% united as agglomerates, these crystallites or agglomerates being bonded by finely divided aluminum oxide, such that the aluminum oxide binder is provided in the reaction as peptizable hydrate; sodium aluminate used as the aluminum and alkali sources; and the primary synthesis of crystalline aluminosilicate effected without acid addition. Catalysts based on pentasil-type crystalline aluminosilicates are formed of primary crystallites of average diameter 0.01-0.1 mu with at least 20% united in 5-500 microns agglomerates, the primary crystallites or agglomerates being bonded together by finely divided aluminum oxide. The catalysts are in H+ form and have BET surface area 300-600 m2/g, pore volume (mercury porosimetry) 0.3-0.8 cm3/g and finely divided aluminum oxide binder content 10-40% based on the total weight of aluminum silicate and binder, and are such that the aluminum oxide binder is provided in the reaction as peptizable aluminum oxide hydrate; sodium aluminate being used as the aluminum and alkali source; and the primary synthesis of crystalline aluminosilicate is effected without acid addition. An Independent claim is also provided for preparation of the catalyst.

Ruthenium hybrid fischer-tropsch catalyst, and methods for preparation and use thereof

Disclosed is a method of forming a hybrid Fischer-Tropsch catalyst extrudate for use in synthesis gas conversion reactions. The method includes extruding a mixture of ruthenium loaded metal oxide support particles, particles of an acidic component and a binder sol to form an extrudate. The resulting extrudate contains from about 0.1 to about 15 weight percent ruthenium based on the weight of the extrudate. In a synthesis gas conversion reaction, the extrudate is contacted with a synthesis gas having a H 2 to CO molar ratio of 0.5 to 3.0 at a reaction temperature of 160° C. to 300° C., a total pressure of 3 to 35 atmospheres, and an hourly space velocity of 5 to 10,000 v/v/hour, resulting in hydrocarbon products containing 1-15 weight % CH 4 ; 1-15 weight % C 2 -C 4 ; 70-95 weight % C 5 + ; 0-5 weight % C 21+ normal paraffins; and 0-10 weight % aromatic hydrocarbons.

Hydrogenation catalyst and use thereof for hydrogenating Fischer-Tropsch endproducts

Catalyst for selective hydrogenation of alkynes in the presence of dienes

Fischer-tropsch catalysts

Catalyst compositions and methods for F-T synthesis which exhibit high CO conversion with minor levels (preferably less than 35% and more preferably less than 5%) or no measurable carbon dioxide generation. F-T active catalysts are prepared by reduction of certain oxygen deficient mixed metal oxides.

Preparation methods for liquid hydrocarbons from syngas by using the zirconia-aluminum oxide-based fischer-tropsch catalysts

A cobalt/zirconia-alumina catalyst in which small pores and large pores coexist by supporting cobalt as an active component on a zirconia-alumina support which comprises ZrO2 and Al2O3 and has a specific surface area by a coprecipitation process, thereby containing the cobalt in the support is provided, and a method for producing liquid hydrocarbons from syngas using the catalyst is provided. In a catalyst for Fischer-Tropsch reaction in which cobalt as an active component is supported on a support, the catalyst for Fischer-Tropsch reaction is characterized in that the catalyst is a catalyst in which cobalt as an active component is supported on a mixed support of zirconia and alumina containing Al2O3 and ZrO2, bimodal structures in which small pores(PS1) with a relatively small pore size and large pores(PS2) with a relatively large pore size coexist are formed in the catalyst, the small pores(PS1) ranges from 2 to 10 nm and the large pores(PS2) ranges from 10 to 200 nm, the ZrO2 is contained in the amount of 1 to 30 wt.% relative to the Al2O3, and the cobalt is contained in the amount of 5 to 40 wt.% relative to the total support. A method for producing liquid hydrocarbons from syngas comprises subjecting syngas to Fischer-Tropsch reaction in the presence of the catalyst for Fischer-Tropsch reaction to produce liquid hydrocarbons. Further, a specific surface of the carrier is 150 to 400 m^2/g and a specific surface of the catalyst is 100 to 300 m^2/g.

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

Porous composite particles are provided which comprise an aluminum oxide component, e.g., crystalline boehmite, and a swellable clay component, e.g., synthetic hectorite, intimately dispersed within the aluminum oxide component at an amount effective to increase the hydrothermal stability, pore volume, and/or the mesopore pore mode of the composite particles relative to the absence of the swellable clay. Also provided is a method for making the composite particles, agglomerate particles derived therefrom, and a process for hydroprocessing petroleum feedstock using the agglomerates to support a hydroprocessing catalyst.

Carrier for ethylene oxide catalysts

An improved carrier for an ethylene epoxidation catalyst is provided. The carrier includes an alumina component containing a first portion of alumina particles having a mean primary particle size of, or greater than, 2 m and up to 6 m, and a second portion of alumina particles having a particle size less than 2 m. An improved catalyst containing the above-described carrier, as well as an improved process for the epoxidation of ethylene using the catalyst are also provided.

Hydrogenation catalysts

Catalysts for hydrogenation comprise a catalytic material and an inorganic matrix component, wherein the catalytic material comprises: at least one metal component comprising a metal selected from the group consisting of copper, manganese, zinc, nickel, cobalt, and iron; and an alkali metal component or an alkaline earth metal component; wherein the inorganic matrix component based on at least a silica sol component and a clay material; wherein the catalytic material and the inorganic matrix component are processed together to form the catalyst; and wherein the catalyst has a mesopore volume in the range of 50-90 by weight % of an overall pore volume. Catalysts are effective for converting acetophenone to methylphenyl carbinol and/or for converting nitrobenzene to aniline.

Aromatization catalysts with high surface area and pore volume

Regenerable aromatization catalysts having high surface area and pore volume, as well as methods for producing these catalysts, are disclosed.

Methods and systems for upgrading heavy oil using catalytic hydrocracking and thermal coking

Methods and systems for hydroprocessing heavy oil feedstocks to form upgraded material use a colloidal or molecular catalyst dispersed within heavy oil feedstock, pre-coking hydrocracking reactor, separator, and coking reactor. The colloidal or molecular catalyst promotes upgrading reactions that reduce the quantity of asphaltenes or other coke forming precursors in the feedstock, increase hydrogen to carbon ratio in the upgraded material, and decrease boiling points of hydrocarbons in the upgraded material. The methods and systems can be used to upgrade vacuum tower bottoms and other low grade heavy oil feedstocks. The result is one or more of increased conversion level and yield, improved quality of upgraded hydrocarbons, reduced coke formation, reduced equipment fouling, processing of a wider range of lower quality feedstocks, and more efficient use of supported catalyst if used with the colloidal or molecular catalyst, as compared to a conventional hydrocracking process or a conventional thermal coking process.

Catalyst

Doped Pd / Au coated catalyst, process for its preparation and its use

Die vorliegende Erfindung betrifft einen Schalenkatalysator für die Herstellung von Vinylacetat-Monomer (VAM), umfassend einen als Formkörper ausgebildeten, oxidischen porösen Katalysatorträger mit einer äußeren Schale, in welcher metallisches Pd und Au enthalten sind. Um einen Schalenkatalysator für die Herstellung von VAM bereitzustellen, der eine verhältnismäßig hohe Aktivität aufweist und relativ kostengünstig erhältlich ist, wird vorgeschlagen, dass der Katalysatorträger mit zumindest einem Oxid eines Elementes, ausgewählt aus der Gruppe, bestehend aus Li, P, Ca, V, Cr, Mn, Fe, Sr, Nb, Ta, W, La und den Seltenerdmetallen dotiert ist. The present invention relates to a coated catalyst for the production of vinyl acetate monomer (VAM), comprising a formed as a shaped body, oxidic porous catalyst support having an outer shell, in which metallic Pd and Au are included. In order to provide a shell catalyst for the production of VAM which has a relatively high activity and is relatively inexpensive to obtain, it is proposed that the catalyst support be provided with at least one oxide of an element selected from the group consisting of Li, P, Ca, V, Cr, Mn, Fe, Sr, Nb, Ta, W, La and the rare earth metals is doped.

Catalysts containing copper-zincoxide-aluminiumoxide

Catalyst for conversion processes

Components and catalysts for the polymerization of olefins

The present invention relates to components of catalysts for the polymerization of olefins comprising a metallocene compound and a magnesium halide which have particular values of porosity and surface area. In particular the components of the invention have surface area (BET) greater than about 50 m 2 /g, porosity (BET) greater than about 0.15 cm 3 /g and porosity (Hg) greater than 0.3 cm 3 /g, with the proviso that when the surface area is less than about 150 m 2 /g, the porosity (Hg) is less than about 1.5 cm 3 /g. The components of the invention are particularly suitable for the preparation of catalysts for the gas-phase polymerization of α-olefins.

Method for producing catalyst for hydrotreating hydrocarbon oil

HYDRO-TREATMENT CATALYST FOR HYDRAULIC OIL AND METHOD OF PRODUCING THEREOF, AND METHOD FOR HYDRO-TREATING HYDRAULIC OIL USED THEREOF

Method for producing hydrotreating catalyst from hydrogel

Process for the preparation of hydrotreating catalysts from hydrogels