ВЫХЛОПНАЯ СИСТЕМА ДЛЯ ДВИГАТЕЛЯ С ВОСПЛАМЕНЕНИЕМ ОТ СЖАТИЯ, ВКЛЮЧАЮЩАЯ ОБЛАСТЬ ЗАХВАТА ИСПАРИВШЕЙСЯ ПЛАТИНЫ

Изобретение относится к выхлопной системе для обработки выхлопных газов двигателя с воспламенением от сжатия, где выхлопная система содержит катализатор окисления, включающий носитель, который представляет собой проточный монолитный носитель или фильтрующий монолитный носитель и имеет поверхность входного конца и поверхность выходного конца; каталитический материал, расположенный на носителе, причем каталитический материал содержит платину (Pt); и зону захвата, содержащую захватывающий материал, где захватывающий материал содержит Pt-легирующий металл, расположенный на тугоплавком оксиде или нанесенный на тугоплавкий оксид, где Pt-легирующий металл в катализаторе окисления является палладием (Pd), причем захватывающий материал расположен на множестве стенок каналов или нанесен на множество стенок каналов внутри носителя, и при этом тугоплавкий оксид включает по меньшей мере 65% вес. оксида циркония, при этом данная зона захвата имеет среднюю длину ≤20 мм, расположена на поверхности выходного ...

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

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

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 ...

КАТАЛИЗАТОРЫ С ВЫСОКОЙ ГЕОМЕТРИЧЕСКОЙ ПЛОЩАДЬЮ ПОВЕРХНОСТИ ДЛЯ ПОЛУЧЕНИЯ ВИНИЛАЦЕТАТНОГО МОНОМЕРА

Изобретение относится к катализатору для получения винилацетатного мономера, содержащему подложку, содержащую внешнюю поверхность, от 60 масс. % до 99 масс. % диоксида кремния и от 1,0 масс. % до 5,0 масс. % оксида алюминия. Каталитический слой размещен в указанной подложке вблизи указанной внешней поверхности, причем указанный каталитический слой содержит Pd, Au и ацетат калия (KOAc). В указанном катализаторе (а) содержание KOAc составляет от 60 кг/мдо 150 кг/мкатализатора, или (b) каталитический слой имеет среднюю толщину от 50 мкм до 150 мкм, или (с) одновременно выполняются условия (а) и (b). Катализатор также имеет площадь поверхности, рассчитанную по методу Брунауэра-Эмметта-Теллера, составляющую от 130 м/г до 300 м/г и геометрическую площадь поверхности на единицу объема каталитического слоя от 550 м/мдо 1500 м/м. Катализатор обладает высокой активностью в отношении синтеза винилацетатного мономера и обладает высокой селективностью по отношению к винилацетатному мономеру. 3 н. и ...

КОМПОЗИЦИЯ С ПОВЫШЕННОЙ КИСЛОТНОСТЬЮ НА ОСНОВЕ ОКСИДОВ ЦИРКОНИЯ, КРЕМНИЯ И, ПО МЕНЬШЕЙ МЕРЕ, ОДНОГО ДРУГОГО ЭЛЕМЕНТА, ВЫБРАННОГО ИЗ ТИТАНА, АЛЮМИНИЯ, ВОЛЬФРАМА, МОЛИБДЕНА, ЦЕРИЯ, ЖЕЛЕЗА, ОЛОВА, ЦИНКА И МАРГАНЦА

... 1. Композиция на основе оксида циркония, оксида кремния и, по меньшей мере, одного оксида другого элемента М, выбранного из титана, алюминия, вольфрама, молибдена, церия, железа, олова, цинка и марганца в следующих массовых пропорциях различных элементов: ! оксид кремния: 5-30%, ! оксид элемента М:1-20%, ! достаточное количество до 100% оксида циркония, ! отличающаяся тем, что она обладает, кроме того, кислотностью, определенную в результате испытания с использованием метилбутанола, равную, по меньшей мере, 90%. ! 2. Композиция по п.1, отличающаяся тем, что элемент М представляет собой вольфрам, и после кальцинации при 900°С в течение 4 ч она обладает удельной поверхностью, равной, по меньшей мере, 65 м2/г. ! 3. Композиция по п.1, отличающаяся тем, что элемент М отличен от вольфрама, и после кальцинации при 900°С в течение 4 ч она имеет удельную поверхность, равную, по меньшей мере, 95 м2/г. ! 4. Композиция по любому из предыдущих пунктов, отличающаяся тем, что она обладает кислотностью ...

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 ...

CATALYST

CATALYST

CATALYST

POROUS INORGANIC MACRO STRUCTURES AND PROCEDURES FOR THE PRODUCTION THE SAME

Transition metal-carbide and nitride containing catalysts , their preparation and use as oxidation and dehydrogenation catalysts

CHROMIUM OXIDE CATALYST FOR GAS PHASE FLUORIDATION

CHROMIUM SULPHATE CATALYST FOR GAS PHASE FLUORIDATION

Catalyst for oxidizing SO2 to SO3 and utilization of the catalyst in a method for producing sulfuric acid

PRODUCTION OF CYCLOHEXANONE

ELECTRODE CATALYST, AND MEMBRANE ELECTRODE ASSEMBLY AND FUEL CELL USING ELECTRODE CATALYST

Provided is a catalyst that can exhibit high activity. An electrocatalyst is formed by catalytic metal being supported by a catalyst support. The catalytic metal includes platinum and a metal component other than platinum. The electrocatalyst has meso holes, which have a radius of 1 nm or greater, with the mode radius of hole distribution for the meso holes being 1 nm or greater and less than 2.5 nm. Alloy microparticles of the platinum and the metal component other than platinum are supported in the meso holes, and the molar ratio for the platinum content with respect to the metal component other than platinum in alloy microparticles supported in the meso holes is 1.0 - 10Ø ...

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

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

CATALYST AND PROCESS FOR THE PRODUCTION OF DIESEL FUEL FROM NATURAL GAS, NATURAL GAS LIQUIDS, OR OTHER GASEOUS FEEDSTOCKS

A process is described that operates efficiently to produce diesel fuel blend from hydrogen and carbon monoxide. The process uses a reduced catalyst on a metal oxide catalyst support which are configured to selectively convert the hydrogen and carbon monoxide into a hydrocarbon product stream, wherein the hydrocarbon product stream comprises light gases, diesel fuel and a wax. These are then condensed, and the diesel fuel blended with a petroleum derived fuel, to produce a diesel fuel blend.

A METHOD OF PREPARING A MESOPOROUS CARBON COMPOSITE MATERIAL COMPRISING METAL NANOPARTICLES AND USE THEREOF AS CATALYST

The present invention relates to a method of preparing a mesoporous carbon composite material comprising a mesoporous carbon phase and preformed metal nanoparticles located within said mesoporous carbon phase. The present invention also relates to a mesoporous carbon composite material and to a substrate comprising a film of such mesoporous carbon composite material. Furthermore, the present invention relates to the use of a mesoporous carbon composite material according to the present invention.

CATALYTICALLY DEGRADABLE PLASTIC AND USE OF SAME

A catalytically degradable plastic is described, with content of cellulose esters and also optionally of additives. A particular characterizing feature of this catalytically degradable plastic is that it contains a dispersed, catalytically active transition-metal-modified titanium dioxide.

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.

COATING METHODS USING ORGANOSILICA MATERIALS AND USES THEREOF

Methods for coating a substrate with a coating including an adsorbent material and a binder comprising an organosilica material which is a polymer comprising independent units of Formula [Z3Z4SiCH2] 3 (I), wherein each Z3 represents a hydroxyl group, a C1-C4 alkoxy group or an oxygen atom bonded to a silicon atom of another unit or an active site on the substrate and each Z4 represents a hydroxyl group, a C1-C4 alkoxy group, a C1-C4 alkyl group, an oxygen atom bonded to a silicon atom of another unit or an active site on the substrate are provided. Methods of gas separation are also provided.

AROMATIC HYDROGENATION CATALYSTS AND USES THEREOF

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

CATALYST AND METHODS OF PRODUCTION DIESEL FUEL FROM NATURAL GAS, LIQUID POSTS FROM NATURAL GAS OR OTHER GASEOUS RAW MATERIAL

STEAM REFORMING CATALYST AND METHOD OF ITS MANUFACTURE

CATALYST

CATALYST AND METHODS FOR PREPARING DIZELNGO FUEL FROM NATURAL GAS, LIQUID POSTS FROM NATURAL GAS OR OTHER GASEOUS RAW MATERIAL

촉매 담체용 탄소 재료

... 촉매 담체로서 사용했을 때, 높은 기공성을 유지하면서, 화학적으로 안정되고, 전기 전도성을 갖고, 내구성이 우수하고, 또한 반응 원료 및 반응 생성물의 확산성도 우수한 촉매 담체용 탄소 재료를 제공한다. 탄소를 포함하는 봉상체 또는 환상체가 갈라져 나온 3차원 구조를 갖는 수상의 탄소 메조포러스 구조체를 포함하고, 질소 흡착 등온선을 돌리모어-힐법으로 해석해서 구해지는 세공 직경 1 내지 20㎚ 및 적산 세공 용적 0.2 내지 1.5cc/g을 갖고, 분말 X선 회절 스펙트럼이, 회절각(2θ:도) 20 내지 30도 사이에, 그래파이트의 002 회절선 상당의 피크를 가지며, 또한 25.5 내지 26.5도에 반값폭이 0.1도 내지 1.0도인 피크를 갖는 것을 특징으로 한다.

SHAPED BODIES CONTAINING METAL-ORGANIC FRAMEWORKS

STEAM REFORMING CATALYST

COMPOSED OF ZEOLITE METHOD TO OBTAIN IT AND CATALYTIC APPLICATION OF THE SAME

Un material catalítico que incluye zeolita microporosa sobre un soporte de oxido inorgánico mesoporoso. La zeolita microporosa puede incluir zeolita b, zeolita Y (incluyendo ôultra estable Yö - USY), modernita, Zeolita L, ZSM-5, ZSM-11, ZSM-12, ZSM-20, q-1, ZSM-23, ZSM-34, ZSM-35, ZSM-48, SSZ-32, PSH-3, MCM-22, MCM-49, MCM-56, ITQ-1, ITQ-2, ITQ-4, ITQ-21, SAPO-5, SAPO-11, SAPO-37, breck-6, ALPO4-5, etc.. El oxido inorgánico mesoporoso puede ser, por ejemplo, silica o silicato. El material catalítico puede ser además modificado introduciendo algunos metales, por ejemplo, aluminio, titanio, molibdeno, níquel, cobalto, hierro, tungsteno, paladio, y platino. Puede ser utilizado para reacciones de acilacion, alquilacion, dimerizacion, oligomerizacion, polimerizacion, hidrogenacion, dehidrogenacion, aromatizacion, isomerizacion, hidrotratamiento, cracking catalítico e hidrocracking. Reivindicacion 1: Una composicion que comprende: a) al menos un tipo de un material cristalino y microporoso con ...

IMPROVED PRECIOUS METAL CATALYST FOR DEBENZYLATION

Disclosed is a catalyst composite containing a metal catalyst and a specifically defined carbon support containing a carbonaceous material. For example, the carbon support may have a total pore surface area of about 800 m2/g or more and about 2,000 m2/g or less where about 20% or less of the total pore surface area is micro pore surface area. Alternatively the carbon support may have a total pore volume of at least about 0.75 cc/g where about 15% or less of the total pore volume is micro pore volume. Alternatively, the carbon support may have a phosphorus content of about 0.75% by weight or less. Also disclosed are methods of making and using the catalyst composite.

Catalyst for the Conversion of Syngas to Olefins and Preparation Thereof

Described is a process for the production of a pillared silicate. The process comprises (i) providing a layered silicate; (ii) interlayer expanding the layered silicate provided in step (i) comprising a step of treating the layered silicate with one or more swelling agents; (iii) treating the interlayer expanded silicate obtained in step (ii) with one or more hydrolyzable silicon containing compounds; (iv) treating the interlayer expanded compound obtained in step (iii) with an aqueous solution to obtain a pillared silicate; (v) removing at least a portion of the one or more swelling agents from the pillared silicate obtained in step (iv); and (vi) impregnating the pillared silicate obtained in step (v) with one or more elements selected from the group consisting of Fe, Ru, Ir, and combinations of two or more thereof. Also described is a pillared silicate optionally obtainable from said process and its use, in particular, in a process for the production of one or more olefins according ...

Transition Metal-Containing Catalysts and Processes for Their Preparation and Use As Oxidation and Dehydrogenation Catalysts

This invention relates to the field of heterogeneous catalysis, and more particularly to catalysts including carbon supports having formed thereon compositions which comprise a transition metal in combination with nitrogen and/or carbon. The invention further relates to the fields of catalytic oxidation and dehydrogenation reactions, including the preparation of secondary amines by the catalytic oxidation of tertiary amines and the preparation of carboxylic acids by the catalytic dehydrogenation of alcohols.

Supported catalyst for conversion of propane to propene and its use in a process for that conversion

A process for the conversion of propane to propene is disclosed wherein a silica chromium catalyst composition is contacted with a propane feed stream and a carbon dioxide. The silica chromium catalyst composition is further disclosed wherein the composition, optionally, includes a promoter component.

SUPPORTED CATALYST FOR CONVERSION OF PROPANE TO PROPENE AND ITS USE IN PROCESS FOR THAT CONVERSION

PROBLEM TO BE SOLVED: To provide a method for catalytic conversion of propane to propene in the presence of carbon dioxide in a surprisingly high propene yield. SOLUTION: In the method for the conversion of propane to propene, a silica chromium catalyst composition is brought into contact with a propane feed stream and carbon dioxide. In the silica chromium catalyst composition, the composition, optionally, includes a promoter component. COPYRIGHT: (C)2009,JPO&INPIT ...

КАТАЛИТИЧЕСКИЕ МАТЕРИАЛЫ И СПОСОБ ИХ ПОЛУЧЕНИЯ

... 1. Каталитический материал, отличающийсятем, что каталитический материал представляет собой мезопористое молекулярное сито с заделкой цеолитом, и каталитический материал является термостойким при температуре не ниже 900°C. 2. Каталитический материал по п.1, отличающийся тем, что каталитический материал имеет удельную площадь поверхности в интервале 1400-500 м2/г, предпочтительно, 1200-600 м2/г. 3. Каталитический материал по п.1, отличающийся тем, что каталитический материал содержит мезопористое молекулярное сито, выбранное из группы M41S, предпочтительно, мезопористое молекулярное сито, выбранное из МСМ-41 или МСМ-48. 4. Каталитический материал по п.1, отличающийся тем, что каталитический материал содержит среднепористый цеолит, выбранный из цеолитов MFI, MTT, TON, AEF, MWW и FER, или крупнопористый цеолит, выбранный из цеолитов BEA, FAU, MOR, предпочтительно, цеолитом является цеолит MFI, MTT, AEF, BEA, MWW или MOR. 5. Каталитический материал по п.4, отличающийся тем, что мезопористым ...

KATALYSATOR UND VERFAHREN ZUR GASPHASENFLUORIERUNG VON CHLORIERTEN ALIPHATISCHEN VERBINDUNGEN

VERFAHREN ZUR OLIGOMERISIERUNG VON OLEFINEN

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

CHROMIUM OXIDE CATALYST FOR GAS PHASE FLUORIDATION

Clean gas stack

A flow-through solid catalyst formed by coating a zeolite material on a metal or ceramic solid substrate, in some embodiments, the solid substrate is formed as flat plates, corrugated plates, or honeycomb blocks.

CATALYSTS FOR THE GASEOUS PHASE FLUORINATION OF CHLORINATED HYDROCARBONS AND ALIPHATIC CHLOROFLUORIDES USING CHROMIUM SULFATE DEPOSITED ON AN ACTIVE CARBONE SUBSTRATE; FLUORINATION PROCESSES MAKING USE OF SAID CATALYSTS

L'invention concerne des catalyseurs de fluoruration en phase gazeuse des hydrocarbures chlorés et chlorofluorés aliphatiques, constitués par un support de charbon actif, présentant une surface spécifique totale supérieure à 1 000 m2/g, dont une surface supérieure à 5 m2/g pour les pores de rayons de 40 à 50 .ANG. et une surface supérieure à 2 m2/g pour les pores de rayons égaux ou supérieurs à 250 .ANG. , imprégné par une solution aqueuse de trioxyde de chrome et séché à une température d'environ 150.degree.C. Elle concerne également un procédé de fluoruration en phase gazeuse des hydrocarbures chlorés et chlorofluorés aliphatiques dans des réacteurs à lit fluidisé, garnis de ces catalyseurs selon l'invention qui présentent l'avantage d'être facile à mettre en forme régulière et de posséder une mésoporosité de même qu'une macroporosité élevées.

CATALYSTS FOR THE GASEOUS PHASE FLUORINATION OF ALIPHATIC CHLORINATED DERIVATIVES USING ACTIVE CARBON IMPREGNATED WITH CHROMIUM SULFATE; FLUORINATION PROCESSES MAKING USE OF SAID CATALYSTS

MEMBRANE FABRICATION METHODS USING ORGANOSILICA MATERIALS AND USES THEREOF

Methods for fabricating a membrane with an organosilica material which is a polymer comprising independent units of Formula [Z3Z4SiCH2]3 (I), wherein each Z3 represents a hydroxyl group, a C1-C4 alkoxy group or an oxygen atom bonded to a silicon atom of another unit or an active site on the support and each Z4 represents a hydroxyl group, a C1-C4 alkoxy group, a C1-C4 alkyl group, an oxygen atom bonded to a silicon atom of another unit or an active site on the support are provided. Methods of removing a contaminant from a hydrocarbon stream are also provided.

SELECTIVE PARTIAL HYDROGENATION OF TERPENES USING A NICKEL-BASED CATALYST

The invention relates to a process for the selective partial hydrogenation of conjugated diene compounds comprising at least one, preferably terminal, diene function and at least one additional carbon-carbon double bond, said process comprising reacting the conjugated diene compounds with hydrogen in the presence of a nickel-NHC based catalyst. The invention also relates to a reaction mixture that can be obtained at the end of the process of the invention and to a catalyst that can be used in the process of the invention. The invention also relates to the use of the reaction mixture of the invention.

COMPOSITIONS FOR REMOVING HYDROCARBONS AND HALOGENATED HYDROCARBONS FROM CONTAMINATED ENVIRONMENTS

The present invention provides a supported catalyst for in situ remediation of soil and/or groundwater contaminated with a halogenated hydrocarbon comprising an adsorbent impregnated with zero valent iron, wherein the adsorbent is capable of adsorbing the halogenated hydrocarbon. This invention further provides a bioremediation composition for in situ bioremediation of soil and/or groundwater contaminated with hydrocarbons, comprising an adsorbent capable of adsorbing said hydrocarbons, a mixture of facultative anaerobes capable of metabolizing said hydrocarbons under sulfate-reduction conditions, a sulfate-containing compound that releases sulfate over a period of time, and a nutrient system for promoting growth of said anaerobes, wherein said nutrient system includes a sulfide scavenging agent.

HIGHLY SINTER-STABLE METAL NANOPARTICLES SUPPORTED ON MESOPOROUS GRAPHITIC PARTICLES AND THEIR USE

The present invention refers to highly sinter-stable metal nanoparticles supported on mesoporous graphitic spheres, the so obtained metal-loaded mesoporous graphitic particles, processes for their preparation and the use thereof as catalysts, in particular for high temperature reactions in reducing atmosphere and cathode side oxygen reduction reaction (ORR) in PEM fuel cells.

CATALYST AND PROCESS FOR THE PRODUCTION OF DIESEL FUEL FROM NATURAL GAS, NATURAL GAS LIQUIDS, OR OTHER GASEOUS FEEDSTOCKS

A unique process and catalyst is described that operates efficiently for the direct production of a high cetane diesel type fuel or diesel type blending stock from stochiometric mixtures of hydrogen and carbon monoxide. This invention allows for, but is not limited to, the economical and efficient production high quality diesel type fuels from small or distributed fuel production plants that have an annual production capacity of less than 10,000 barrels of product per day, by eliminating traditional wax upgrading processes. This catalytic process is ideal for distributed diesel fuel production plants such as gas to liquids production and other applications that require optimized economics based on supporting distributed feedstock resources.

STEAM REFORMING CATALYST AND METHOD OF MAKING THEREOF

CATALYST AND METHODS FOR PREPARING DIZELNGO FUEL FROM NATURAL GAS, LIQUID POSTS FROM NATURAL GAS OR OTHER GASEOUS RAW MATERIAL

Bamboo joint/coated non-noble metal SO2 electrochemical oxidation catalyst as well as preparation method and application thereof

Porous graphene material and preparation method and application thereof

MANUFACTORING PROCESS OF FORMALDEHYDE BY SELECTIVE OXIDATION OF METHANE

MANUFACTORING PROCESS OF FORMALDEHYDE BY SELECTIVE OXIDATION OF METHANE

Ce procédé en une seule étape de fabrication du formaldéhyde par oxydation sélective du méthane en phase gazeuse en présence d'un catalyseur dont l'espèce active est constituée par du vanadium et qui est supporté sur du dioxyde de silicium. SiO2 est caractérisé par le fait qu'au moins 50% du vanadium est présent dans le catalyseur sous la forme d'au moins une espèce monomérique.

Porous carbon and method for preparing the same

PROCESS FOR MANUFACTURING A CATALYST SUPPORT AND A CATALYST

The invention relates to a process for manufacturing a catalyst support, in which one or more fibres are fed into a mould, said fibre having a diameter in the range of 5-300 microns, and a length over diameter ratio greater than 500. The body in the mould is compressed and then contacted with a mixture comprising a liquid and a carrier material. The liquid is removed from the wetted body to provide a catalyst support comprising an entangled fibre and carrier material. A catalyst can be made using the same process and additionally adding a catalytically active metal with the mixture comprising a liquid and a carrier material. Alternatively a catalyst can be made using the process for manufacturing a catalyst support followed by impregnation with a catalytically active metal.

CATALYST CARRIER BODY

In order to obtain a particularly effective and long-living catalyst carrier body useful for decomposing by catalysis individual parts of gaseous or aerosol mixtures in gas streams, in particular for decomposing by catalysis the hydrogen peroxide contained in the air, the catalyst carrier body has a supporting body of carbon particles mutually linked without any binders. The carbon particles comprise a first coal fraction forming the supporting structure having a particle size of between 500 and 5000 mum an intermediate pore width of the supporting structure between 50 and 1000 mum and an inner surface of the particles of between 0 and 100m2/cm3, and a second coal fraction of highly-porous activated carbon with an inner surface of between 600 and 3500m2/cm3 and a particle size of between 0.1 and 500 mum. The activated carbon particles are deposited in the intervals between the particles of the first coal fraction, and an inorganic catalytic substance, in particular noble metals and their ...

TUNGSTEN PROMOTED CATALYST FOR CARBONYLATION OF LOWER ALKYL ALCOHOLS

A solid carbonylation catalyst useful for producing esters and carboxylic acids from reactants including lower alkyl alcohols and lower alkyl alcohol producing compositions in a vapor phase carbonylation process wherein the catalyst includes a catalytically effective amount of a Group VIII metal selected from platinum or palladium, and tungsten which are associated with a solid catalyst support material.

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 Brunauer, Emmett, and Teller method is equal to or larger than 10 m2/g, and a volume of a fine pore based on a BJH, namely Barrett, Joyner, and Halenda method and an MP, namely Micro Pore method is equal to or larger than 0.1 cm3/g.

OLIGOMERIZATION CATALYST AND PROCESS FOR THE PRODUCTION THEREOF

The invention relates to an oligomerization catalyst comprising nickel oxide and silica-alumina support material and to a process for oligomerization of C- to C-olefins using the oligomerization catalyst. 1. An oligomerization catalyst comprising nickel oxide , an Al-containing and Si-free binder (<0.1% by weight Si) and an amorphous silica-alumina support material , wherein the catalyst has a composition of from 15% to 40% by weight of NiO , from 10% to 30% by weight of AlO , from 55% to 70% by weight of Sift and from 0.01% to 2.5% by weight of an alkali metal oxide , wherein the oligomerization catalyst has a ratio of tetrahedrally coordinated aluminium atoms to octahedrally coordinated aluminium atoms of 55:45 to 75:25 , determined by Al MAS NMR.2. The oligomerization catalyst according to claim 1 , wherein the oligomerization catalyst has a specific BET surface area of from 150 to 400 m/g claim 1 , determined by nitrogen physisorption.3. The oligomerization catalyst according to claim 1 , wherein the oligomerization catalyst has mesopores and macropores.4. The oligomerization catalyst according to claim 3 , wherein the mesopores of the oligomerization catalyst have an average pore diameter of from 5 to 15 nm determined by mercury porosimetry.5. The oligomerization catalyst according to claim 3 , wherein the macropores of the oligomerization catalyst have an average pore diameter of from 1 to 100 μm determined by mercury porosimetry.6. The oligomerization catalyst according to claim 1 , wherein the oligomerization catalyst is in the form of granulate.7. The oligomerization catalyst according to claim 1 , wherein the oligomerization catalyst has an average particle diameter (d50) of from 0.1 mm to 7 mm claim 1 , determined by imaging methods according to ISO 13322-1 (2004-12-01 version) and ISO 13322-2 (2006-11-01 version).8. A process for oligomerization of C- to C-olefins claim 1 , wherein an olefin-containing feed mixture containing the C-to C-olefins is passed ...

Base metal catalyst for treatment of ozone and volatile organic compounds present in air supply

Disclosed herein are base metal catalyst devices for removing ozone, volatile organic compounds, and other pollutants from an air flow stream. A catalyst device includes a housing, a solid substrate disposed within the housing, and a catalyst layer disposed on the substrate. The catalyst layer includes a first base metal catalyst at a first mass percent, a second base metal catalyst at a second mass percent, and a support material impregnated with at least one of the first base metal catalyst or the second base metal catalyst. The preferred catalyst composition is a combination of manganese oxide and copper oxide.

鉄ドープ炭素の製造方法

... 【課題】本発明は、元素状態の金属、すなわち、酸化状態0の金属を炭素に基づく担持材料上へ施すことができる方法を提供することをその目的とする。 【解決手段】上記目的は、少なくとも1種の元素状態の金属を得る目的で、少なくとも1種の担持材料上に少なくとも1種の酸化状態0の金属を含む少なくとも1種の化合物を気相蒸着する工程、及び少なくとも1種の酸化状態0の金属を含む少なくとも1種の化合物を熱分解する工程を実施することにより、炭素に基づく少なくとも1種の担持材料上に少なくとも1種の元素状態の金属を含む金属ドープ担持材料を製造する方法であって、その蒸着及び分解の工程の間及び工程後に、担持材料をその製造の際に還元化合物と直接接触させないことを特徴とする方法により達成される。 【選択図】図1 ...

ВОЛЬФРАМКАРБИДНЫЕ КАТАЛИЗАТОРЫ НА МЕЗОПОРИСТОМ УГЛЕРОДНОМ НОСИТЕЛЕ, ИХ ПОЛУЧЕНИЕ И ПРИМЕНЕНИЯ

... 1. Вольфрамкарбидный катализатор на мезопористом углеродном носителе, в котороммезопористый углерод является носителем, который имеет высокую площадь поверхности и большой объем пор;вольфрамкарбидные катализаторы диспергированы на поверхности или в каналах углеродного носителя;металлический компонент W составляет от 1 до 80 мас.% катализатора и, в частности, от 30 до 42 мас.%.2. Катализатор по п.1, в котором металлический компонент Ni промотора составляет от 0,1 до 30 мас.% катализатора и, в частности, от 2 до 5 мас.%.3. Катализатор по п.1, в котором носителями являются аморфный мезопористый углерод МС, MC-R и упорядоченный мезопористый углерод СМК-3, СМК-8.4. Катализатор по п.1, в котором носитель синтезируют способом нанолитья; твердыми матрицами являются коммерческий силиказоль или силиказоль с диаметром 5-100 нм, упорядоченный SBA-15 и KIT-6; углеродными предшественниками являются сахароза, фенольная смола, мезофазный пек, фурфуриловый спирт или их смесь; 1 г твердой матрицы пропитывают ...

КАТАЛИЗАТОР С БИМОДАЛЬНЫМ РАСПРЕДЕЛЕНИЕМ ПОР, СПОСОБ ЕГО ПОЛУЧЕНИЯ ПУТЕМ ПЕРЕМЕШИВАНИЯ С АКТИВНОЙ ФАЗОЙ И ЕГО ПРИМЕНЕНИЕ В ГИДРООБРАБОТКЕ УГЛЕВОДОРОДНЫХ ОСТАТКОВ

Sulfur-Doped Carbonaceous porous materials

Catalyst for oxidizing SO2 to SO3 and utilization of the catalyst in a method for producing sulfuric acid

Process of catalytic production of diesel fuel

Atty Dkt: GR-006.02 A unique process and catalyst is described that operates efficiently for the direct production of a high cetane diesel type fuel or diesel type blending stock from stochiometric mixtures of hydrogen and carbon monoxide. This invention allows for, but is not limited to, the economical and efficient production high quality diesel type fuels from small or distributed fuel production plants that have an annual production capacity of less than 10,000 barrels of product per day, by eliminating traditional wax upgrading processes. This catalytic process is ideal for distributed diesel fuel production plants such as gas to liquids production and other applications that require optimized economics based on supporting distributed feedstock resources. WO 2014/137473 PCT/US2014/000026 ...

CHROMIUM SULPHATE CATALYST FOR GAS PHASE FLUORIDATION

CATALYST AND PROCESS FOR THE PRODUCTION OF DIESEL FUEL FROM NATURAL GAS, NATURAL GAS LIQUIDS, OR OTHER GASEOUS FEEDSTOCKS

POROUS GRAPHENE OXIDE MATERIALS

A method of preparing a porous graphene oxide material. The method includes the steps of: (1) preparing graphene oxide sheets from graphite at 40 to 170 °C; (2) providing a graphene oxide suspension containing the graphene oxide sheets; (3) heating the graphene oxide suspension with a base at 25 to 300 °C for 0.1 to 48 hours to obtain base-treated graphene oxide sheets; and (4) heating a mixture of the base-treated graphene oxide sheets and an acid at 25 to 300 °C for 0.1 to 48 hours to yield the porous graphene oxide material. Also disclosed are novel porous graphene oxide materials and methods of using these materials as catalysts.

USE OF MESOPOROUS GRAPHITE PARTICLES FOR ELECTROCHEMICAL APPLICATIONS

The present invention relates to the use of mesoporous graphite particles loaded with sinter-stable metal nanoparticles for fuel cells and other electrochemical applications, such as for use as a component of layers for electrodes of fuel cells and batteries.

SOLAR-ACTIVATED PHOTOCHEMICAL PURIFICATION OF FLUIDS

Disclosed herein are embodiments of a solar- activated photochemical fluid treatment system, some of which comprise a fluid vessel, a porous enclosure positioned inside of the fluid vessel, a fiber substrate contained within the enclosure, and a semiconductor photocatalyst coupled to the fiber substrate. The fluid vessel can be configured to contain a fluid in contact with the photocatalyst such that the fluid treatment system, responsive to solar radiation applied to the photocatalyst and to the fluid in the vessel, induces photochemical modification of contaminants and living organisms in the fluid. Related methods are also disclosed.

COMPOSITIONS FOR REMOVING HYDROCARBONS AND HALOGENATED HYDROCARBONS FROMCONTAMINATED ENVIRONMENTS

The present invention provides a supported catalyst for in situ remediation of soil and/or groundwater contaminated with a halogenated hydrocarbon comprising an adsorbent impregnated with zero valent iron, wherein the adsorbent is capable of adsorbing the halogenated hydrocarbon. This invention further provides a bioremediation composition for in situ bioremediation of soil and/or groundwater contaminated with hydrocarbons, comprising an adsorbent capable of adsorbing said hydrocarbons, a mixture of facultative anaerobes capable of metabolizing said hydrocarbons under sulfate-reduction conditions, a sulfate-containing compound that releases sulfate over a period of time, and a nutrient system for promoting growth of said anaerobes, wherein said nutrient system includes a sulfide scavenging agent.

Cobalt piece supported composite photocatalytic material of ZnO nanoneedles and ZIF-67 as well as preparation and application of cobalt piece supported composite photocatalytic material

High-efficiency ozone removing material

CATALYST WITH AN EXTERNAL SHAPE FOR IMPROVED HYDRODYNAMIC REACTORS

MATERIAL PHOTOCATALYTIQUE ULTRA-POREUX, MANUFACTORING PROCESS AND USES

La présente invention concerne un procédé de fabrication de matériaux photocatalytiques ultra-poreux, les matériaux photocatalytiques ultra-poreux obtenus selon un tel procédé, ainsi que leurs utilisations pour produire de l'hydrogène, traiter les eaux usées et polluées, traiter l'air pollué, ou encore leur utilisation comme membranes catalytiques dans des piles à combustible. Enfin, un dernier objet de l'invention concerne des articles choisis parmi les dispositifs de production d'hydrogène, les vitres autonettoyantes et les murs anti-pollution.

NANOZEOLITE SUPPORTING TRIVALENT IRON IONS, AND PREPARATION METHOD THEREOF

The present invention relates to nanozeolite supporting trivalent iron ions (Fe^(3+)), and to a water treatment method using the same. The nanozeolite of the present invention has an average particle size at nanolevel, and supports Fe^(3+), thereby having a large specific surface area. Also, the nanozeolite has excellent adhesive strength regarding aromatic organic compounds. Thus, a water treatment method and a water treatment apparatus using the nanozeolite are useful for water treatment of industrial and agricultural wastewater. COPYRIGHT KIPO 2016 (CC) Example 2 (DD) Example 1 (EE) Comparative example 1 (BB) Example 3 (AA) Strength (2) θ[ ] ...

Porous carbon material, method for producing the same, and catalyst for synthesis reaction

A porous carbon material, wherein the full width at half maximum (2[Theta]) for the diffraction peak (10X) (38 DEG to 49 DEG) obtained by x-ray diffraction is not more than 4.2 DEG, and the ratio (mesopore volume/micropore volume) between the mesopore volume (cm3/g) as measured by the BJH method and the micropore volume (cm3/g) as measured by the HK method is at least 1.20.

PROCESS FOR PREPARING CATALYSTS USEFUL IN DIRECT LIQUEFACTION OF CARBON, AND THE RESULTING CATALYST

The present invention relates to a method for obtaining transition-metal catalysts supported on a carbonaceous material via impregnation with a solution from the thiourea metal complex, obtained from the precursor salts. Sulphur is formed on the surface of the substrate by thermal decomposition of the complex. The catalysts obtained by means of the process of the present invention are applicable to the direct liquefaction of carbon.

GOLD CATALYSTS AND THE USE THEREOF IN THE WATER-GAS SHIFT REACTION

The present invention relates to a substrate for a gold catalyst, of formula CeO2 - ΜΟχ/ΑΙ2O3, wherein the substrate comprises between 60 and 90% w/w of Al2O3 and a percentage of CeO2 between 10 and 40% w/w, optionally doped with MOx oxide, with M selected from Fe, Zn, Co and Ni, Zr or mixtures thereof. The present invention relates to the use of the catalyst for the water-gas shift reaction and, more particularly, the use thereof in fuel cells.

Selective isomerization of olefins to alkenes using a mesoporous catalyst

A process for selectively making 2-alkenes from a NAO using a mesoporous catalyst that has been surface modified with a Brönsted acid compound. The Brönsted acid compound has a reactive silane connector, an organic linking group, and a Brönsted acid group. The mesoporous catalyst has an average pore diameter in a range of about 12 to about 100 Angstroms and a surface area of between about 400 to about 1400 m2/gram.

High geometric surface area catalysts for vinyl acetate monomer production

A catalyst includes a support, where the support includes an external surface, about 60 wt % to about 99 wt % silica, and about 1.0 wt % to about 5.0 wt % alumina. A catalytic layer is disposed within the support adjacent to the external surface, where the catalytic layer further includes Pd, Au, and potassium acetate (KOAc). In the catalyst, (a) the KOAc is from about 60 kg/m3 to about 150 kg/m3 of the catalyst; or (b) the catalytic layer has an average thickness from about 50 μm to about 150 μm; or (c) both (a) and (b). The catalyst also possesses a Brunauer-Emmett-Teller surface area of about 130 m2/g to about 300 m2/g and a geometric surface area per packed bed volume from about 550 m2/m3 to about 1500 m2/m3. The catalyst is highly active for the synthesis of vinyl acetate monomer and exhibits a high selectivity for vinyl acetate monomer.

Mesoporous carbon supported copper based catalyst, production and use thereof

This invention relates to a mesoporous carbon supported copper based catalyst comprising mesoporous carbon, a copper component and an auxiliary element supported on said mesoporous carbon, production and use thereof. The catalyst is cheap in cost, friendly to the environment, and satisfactory in high temperature resistance to sintering, with a highly improved and a relatively stable catalytic activity.

NEW ORGANOMETALLIC FRAMEWORK MATERIALS BASED ON ALUMINUM, IRON, AND CHROMIUM

ВОЛЬФРАМКАРБИДНЫЕ КАТАЛИЗАТОРЫ НА МЕЗОПОРИСТОМ УГЛЕРОДНОМ НОСИТЕЛЕ, ИХ ПОЛУЧЕНИЕ И ПРИМЕНЕНИЯ

Изобретение относится к вольфрамкарбидному катализатору на мезопористом углеродном носителе для прямой каталитической конверсии целлюлозы в этиленгликоль, в котором носителем является мезопористый углерод; вольфрамкарбидные катализаторы диспергированы на поверхности или в каналах углеродного носителя; металлический компонент W составляет от 1 до 80% масс. катализатора и, в частности, от 30 до 42% масс. Также изобретение относится к способу получения катализатора пропиткой мезопористого углеродного носителя раствором соли вольфрама и никеля или вольфрама и применению катализатора. Технический результат заключается в получении катализатора для превращения целлюлозы в этиленгликоль с высоким выходом и селективностью. 3 н. и 7 з.п. ф-лы, 3 ил., 3 табл., 7 пр.

КОБАЛЬТ-МОЛИБДЕНОВЫЙ КАТАЛИЗАТОР НА УГЛЕРОДНОЙ ПОДЛОЖКЕ

... 1. Каталитическая композиция, включающая кобальт (Co); и молибден (Mo) на подложке активированного угля (C), причем относительные молярные соотношения элементов, входящих в состав указанной композиции, представлены формулой:CoMoMCпричем:M представляет собой один или несколько элементов,выбранных из группы, состоящей из щелочных металлов ищелочноземельных металлов;a равен 1Е-3 - 0,3;b равен 1Е-3 - 0,9;c равен 0 - 1Е-2; ипри этом указанные Co и Mo находятся в металлической форме, и при этом указанная каталитическая композиция имеет площадь поверхности по БЭТ по меньшей мере 320 м/г.2. Каталитическая композиция по п.1, отличающаяся тем, что M выбран из группы, состоящей из калия (K), натрия (Na), кальция (Ca) и магния (Mg).3. Каталитическая композиция по п.1, отличающаяся тем, что:а равен 1Е-2 - 0,3; иb равен 5Е-3 - 0,9.4. Каталитическая композиция по п.1, отличающаяся тем, что указанная каталитическая композиция имеет площадь поверхности по БЭТ 350-1200 м/г.5. Каталитическая композиция по ...

Verfahren zur Herstellung von Amiden aus Oximen

Verfahren zur Farbzahlverbesserung von Trimethylolpropan

Die vorliegende Erfindung betrifft ein Verfahren zur Herstellung von Trimethylolpropan mit geringer Farbzahl durch Aktivkohlebehandlung.

An iron oxide/vanadate catalyst for the oxidation of sulfur dioxide in the manufacture of sulfuric acid

The catalyst has a porous carrier with a BET surface area of 100-2000 m<2>/g and active components containing at least 80 wt.% iron oxides and at least 5% vanadium as vanadate. The carrier may be a zeolite or meso-porous silicon dioxide. In a preliminary contact stage in a H2SO4 manufacturing plant a gas consisting of O2/SO2 in a volume ratio of at least 1:2 is brought into contact with a bed of the granular catalyst at 580-800 deg C. This converts between 20 and 80% of the SO2 to SO3. This gas is cooled and passed into an absorber. The gas leaving the absorber is heated to 380-600 deg C and with an SO2 concentration of 10 to 30 vol.% is catalytically converted to SO3 at 480-770 deg C in a 2nd oxidation stage. This SO3 is extracted for the manufacture of H2SO4.

A chromium catalyst, its preparation and use

Disclosed is a chromium oxide catalyst. The catalyst comprises a chromium (III) oxide and chromium (VI) oxide. The chromium (VI) is present at a concentration of 10000 ppm or less based on total chromium oxide content. The chromium oxides are present at 96 wt% or more of the catalyst. The bulk density of the catalyst is between 0.3 g/cc and 1 g/cc. Preferably the chromium oxide catalyst may take the form of pellets, beads, extrudates, rings, spheres, cylinders, trilobe or quadralobe shaped pieces. The catalyst may be in contact with a substrate. The catalyst may also comprise a co-catalyst.

Na-Y Molecular Sieve, H-Y Molecular Sieve, and preparation methods thereof, hydrocracking catalyst, and hydrocracking method

Metal-organic framework compounds and their method of manufacture

Na-Y Molecular Sieve, H-Y Molecular Sieve, and preparation methods thereof, hydrocracking catalyst, and hydrocracking method

The present invention discloses 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 1-10nm diameter accounts for 70-90% of the total pore volume of the Na-Y molecular sieve. It may be prepared by mixing sodium silicate, high and low alkaline sodium meta-aluminate and aluminium sulphate at a certain mole ratio, aging to obtain a gel, and treating the gel by hydrothermal crystallisation. 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 ...

A chromium catalyst, its preparation and use

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

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

PROCESSING OF HEAVY HYDROCARBON FEEDS

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

ELECTRODE CATALYST FOR FUEL BATTERY, ELECTRODE CATALYST LAYER OF FUEL BATTERY, MEMBRANE-ELECTRODE ASSEMBLY, AND FUEL BATTERY

An electrode catalyst for a fuel battery includes a mesoporous material and catalyst metal particles supported at least in the mesoporous material. In the electrode catalyst for a fuel battery, before supporting the catalyst metal particles, the mesoporous material has mesopores having a mode radius of greater than or equal to 1 nm and less than or equal to 25 nm and has a value of greater than 0.90, the value being determined by dividing a specific surface area S(m/g) of the mesopores obtained by analyzing a nitrogen adsorption-desorption isotherm according to a BJH method, the mesopores having a radius of greater than or equal to 1 nm and less than or equal to 25 nm, by a BET specific surface area (m/g) evaluated according to a BET method. 1. An electrode catalyst for a fuel battery , comprising:a mesoporous material; andcatalyst metal particles supported at least in the mesoporous material,wherein, before supporting the catalyst metal particles,{'sub': '1-25', 'sup': 2', '2, 'the mesoporous material has mesopores having a mode radius of greater than or equal to 1 nm and less than or equal to 25 nm and has a value of greater than 0.90, the value being determined by dividing a specific surface area S(m/g) of the mesopores obtained by analyzing a nitrogen adsorption-desorption isotherm according to a BJH method, the mesopores having a radius of greater than or equal to 1 nm and less than or equal to 25 nm, by a BET specific surface area (m/g) evaluated according to a BET method.'}2. The electrode catalyst for a fuel battery according to claim 1 ,wherein the mesopores of the mesoporous material have a mode radius of greater than 1.65 nm.3. The electrode catalyst for a fuel battery according to claim 1 ,{'sup': '2', 'wherein the BET specific surface area of the mesoporous material is greater than or equal to 1500 (m/g).'}4. The electrode catalyst for a fuel battery according to claim 1 ,wherein, among the catalyst metal particles supported in the mesoporous material, ...

USE OF MANGANESE OXIDE AND ACTIVATED CARBON FIBERS FOR REMOVING A PARTICLE, VOLATILE ORGANIC COMPOUOND OR OZONE FROM A GAS

The present invention provides for a device for reducing a volatile organic compound (VOC) content of a gas comprising a manganese oxide (MnO) catalyst. The manganese oxide (MnO) catalyst is capable of catalyzing formaldehyde at room temperature, with complete conversion, to COand water vapor. The manganese oxide (MnO) catalyst itself is not consumed by the reaction of formaldehyde into COand water vapor. The present invention also provides for a device for reducing or removing a particle, a VOC and/or ozone from a gas comprising an activated carbon filter (ACF) on a media that is capable of being periodically regenerated. 19.-. (canceled)10. A method for reducing formaldehyde content of a gas , comprising:{'sup': 2', '−1, 'at room temperature, contacting the formaldehyde-containing gas with a manganese-containing catalyst comprising majority non-stoichiometric manganese oxide-hydroxide particles having a Brunner Emmet and Teller (BET) surface area of at least 100 mg, thereby obtaining a gas having a reduced formaldehyde content as compared to the gas prior to contact with the manganese-containing catalyst.'}11. The method of claim 10 , wherein the manganese-containing catalyst comprises majority nsutite.12. The method of claim 10 , wherein the manganese-containing catalyst comprises greater than 90% nsutite.13. The method of claim 10 , wherein the manganese-containing catalyst comprises greater than 95% nsutite.14. The method of claim 10 , wherein the manganese-containing catalyst further comprises cryptomelane.15. The method of claim 11 , wherein the manganese-containing catalyst further comprises cryptomelane.16. The method of claim 12 , wherein the manganese-containing catalyst further comprises cryptomelane.17. The method of claim 12 , wherein the manganese-containing catalyst consists essentially of nsutite and cryptomelane particles.18. The method of claim 13 , wherein the manganese-containing catalyst consists essentially of nsutite and cryptomelane ...

ACTIVATED CARBON WITH A SPECIAL FINISHING, PRODUCTION AND USE THEREOF

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

HIGHLY DISPERSED METAL CATALYST AND RELATED METHODS

Supported catalysts having an atomic level single atom structure are provided such that substantially all the catalyst is available for catalytic function. Processes of forming a catalyst unto a porous catalyst support is also provided. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. A process of forming a catalytic metal onto a catalyst support , the process comprising the steps of:preparing an aqueous solution comprising a catalytic metal and a promoter to form a catalyst and promoter solution, the promoter having an opposite charge of a charge of the catalytic metal;selecting a porous catalyst support with adequate surface area;adjusting the pH of the resulting catalyst and promoter solution in accordance with surface properties of the porous catalyst support;immersing the catalyst support in the solution;removing the catalyst support from the solution;drying the catalyst support under conditions that prevents capillary effect transfer of the solution from an interior of the catalyst support to an exterior of the catalyst support; andperforming a catalyst calcination step under elevated temperatures.11. The process according to wherein the catalytic metal is selected from the group consisting of transition metals claim 10 , noble metals and metallic compounds.12. The process according to wherein the transition metals claim 11 , noble metals and metallic compounds consist of any transition metal or noble metal in the periodic table groups VIII claim 11 , groups IIIB-VIIB and groups IB-2B.13. (canceled)14. The process according to wherein the step of immersing the catalyst support in the solution comprises immersing the catalyst support in the solution such that the porous catalyst support is impregnated with the catalytic metal.15. The process according to wherein the catalyst support is in contact with the catalyst and promoter solution for impregnation.16. The process according to wherein ...

PROCESS FOR USING IRON AND PARTICULATE CARBON CATALYST FOR SLURRY HYDROCRACKING

A process and catalyst is disclosed for converting heavy hydrocarbon feed into lighter hydrocarbon products using multifunctional catalysts. Multifunctional catalysts enable use of less expensive metal by substituting expensive metals for less expensive metals with no loss or superior performance in slurry hydrocracking. Less available and expensive ISM can be replaced effectively. 1. A process for converting heavy hydrocarbon feed into lighter hydrocarbon products comprising:mixing said heavy hydrocarbon liquid feed with catalyst and hydrogen to form a heavy hydrocarbon slurry comprising hydrocarbon liquid and catalyst particles, said catalyst comprising iron and carbon particles comprising a pore volume of at least about 0.12 cc/g, and a mean diameter of no more than about 800 microns;hydrocracking hydrocarbons in said heavy hydrocarbon slurry in the presence of hydrogen and catalyst in a hydrocracking reactor to produce a hydrocracked slurry product comprising lighter hydrocarbon products; andwithdrawing said hydrocracked slurry product from said hydrocracking reactor.2. The process of wherein the iron is impregnated on the carbon particles.3. The process of wherein the iron is provided as bauxite claim 1 , red mud claim 1 , iron sulfate claim 1 , limonite claim 1 , laterite or iron salt particles.4. The process of wherein the iron in the catalyst is no more than about 0.7 wt % in the feed.5. The process of wherein the carbon particles have a mean diameter of no more than about 150 microns.6. The process of wherein the micropore volume of the carbon particles is less than about 0.5 cc/g.7. The process of wherein the BET surface area of the carbon particles is at least about 200 m/g.8. The process of wherein the carbon particles comprise no more than about 2 wt % of the feed to the reactor.9. The process of wherein the iron is provided as bauxite and the iron in the catalyst is no more than about 0.4 wt % in the feed.10. The process of wherein the yield of TIOR in ...

PROCESS FOR USING MOLYBDENUM AND PARTICULATE CARBON CATALYST FOR SLURRY HYDROCRACKING

A process and catalyst is disclosed for converting heavy hydrocarbon feed into lighter hydrocarbon products using multifunctional catalysts. Multifunctional catalysts enable use of less expensive metal by substituting expensive metals for less expensive metals with no loss or superior performance in slurry hydrocracking. Less available and expensive ISM can be replaced effectively. 1. A process for converting heavy hydrocarbon feed into lighter hydrocarbon products comprising:mixing said heavy hydrocarbon liquid feed with catalyst and hydrogen to form a heavy hydrocarbon slurry comprising hydrocarbon liquid and catalyst particles, said catalyst comprising molybdenum and carbon particles comprising pore volume of at least 0.2 cc/g, and a mean diameter of no more than 800 microns;hydrocracking hydrocarbons in said heavy hydrocarbon slurry in the presence of hydrogen and catalyst in a hydrocracking reactor to produce a hydrocracked slurry product comprising lighter hydrocarbon products; andwithdrawing said hydrocracked slurry product from said hydrocracking reactor.2. The process of wherein the molybdenum is impregnated on the carbon particles.3. The process of wherein the molybdenum is provided as molybdenum sulfide in the hydrocracking reactor.4. The process of wherein the molybdenum in the catalyst is no more than about 200 wppm in the feed.5. The process of wherein the carbon particles have a mean diameter of no more than 150 microns.6. The process of wherein the micropore volume of the carbon particles is less than 0.5 cc/g.7. The process of wherein the BET surface area of the carbon particles is at least 200 m/g.8. The process of wherein the carbon particles comprise no more than 2 wt % in the feed.9. The process of wherein the molybdenum is no more than about 175 wppm in the feed.10. The process of wherein the yield of TIOR in the product is no more than about 3.0 wt % of the feed.11. The process of wherein the yield of mesophase in the product is no more than ...

CERIUM OXIDE PARTICLES AND METHOD FOR PRODUCTION THEREOF

The present invention relates to cerium oxide particles that have excellent heat resistance under hydrothermal conditions at high temperature. The present invention also relates to a method for preparing such cerium oxide particles and to a catalytic composition comprising said cerium oxide. 1. Cerium oxide particles exhibiting:{'sub': 2', '2', '2, 'sup': '2', 'a specific surface area (BET) after ageing at 800° C. for 16 hours, under a gaseous atmosphere containing 10% by volume of O, 10% by volume of HO and the balance of N, of at least 75 m/g; or'}{'sub': 2', '2', '2, 'sup': '2', 'a specific surface area (BET) after ageing at 700° C. for 16 hours, under a gaseous atmosphere containing 10% by volume of O, 10% by volume of HO and the balance of N, of at least 97 m/g.'}2. Cerium oxide particles according to claim 1 , exhibiting a specific surface area (BET) after ageing at 800° C. for 16 hours claim 1 , under a gaseous atmosphere containing 10% by volume of O claim 1 , 10% by volume of HO and the balance of N claim 1 , between 75 and 80 m/g.3. Cerium oxide particles according to claim 1 , exhibiting a specific surface area (BET) after ageing at 700° C. for 16 hours claim 1 , under a gaseous atmosphere containing 10% by volume of O claim 1 , 10% by volume of HO and the balance of N.4. Cerium oxide particles according to claim 1 , exhibiting a specific surface area (BET) after ageing at 700° C. for 16 hours claim 1 , under a gaseous atmosphere containing 10% by volume of O claim 1 , 10% by volume of HO and the balance of N claim 1 , between 97 and 102 m/g.5. Cerium oxide particles according to one of the preceding claims claim 1 , exhibiting a specific surface area (BET) after ageing at 900° C. for 16 hours claim 1 , under a gaseous atmosphere containing 10% by volume of O claim 1 , 10% by volume of HO and the balance of N claim 1 , of at least 39 m/g.6. Cerium oxide particles according to claim 1 , exhibiting a specific surface area (BET) after ageing at 900° C. for ...

WATER STABLE COPPER PADDLEWHEEL METAL ORGANIC FRAMEWORK (MOF) COMPOSITIONS AND PROCESSES USING THE MOFS

This invention relates to a Cu-BTC MOF which is water stable. The Cu-BTC MOF has been modified by substituting some of the BTC ligand (1,3,5, benzene tricarboxylic acid) with 5-aminoisophthalic acid (AIA). The resultant MOF retains at least 40% of its as synthesized surface area after exposure to liquid water at 60° C. for 6 hours. This is an unexpected result versus the MOF containing only the BTC ligand. This MOF can be used to abate contaminants such as ammonia in gas streams and especially air streams. 1. A metal organic framework (MOF) composition comprising:a coordination product of a copper metal ion and a mixture of organic ligands selected from 1,3,5-benzenetricarboxylic acid (BTC) and 5-aminoisophthalic acid (AIA) the MOF characterized in that it retains at least 40% of its as synthesized surface area after exposure to liquid water at 60° C. for 6 hours.2. The composition of further characterized in that the MOF has an as synthesized Brunauer-Emmett-Teller (BET) surface area of at least 1500 m/g.3. The composition of further characterized in that the MOF has an as synthesized Brunauer-Emmett-Teller (BET) surface area of at least 1700 m/g.4. The composition of further characterized in that the MOF has a gravimetric uptake capacity for ammonia of at least 0.25 g of ammonia per gram of MOF measured at 650 torr and 25° C.5. The composition of where the molar ratio of BTC:AIA varies from about 99:1 to about 1:99.6. The composition of where the molar ratio of BTC:AIA is 1:1.7. The composition of where the molar ratio of BTC:AIA is 1:38. The composition of where the molar ratio of BTC:AIA is: 3:1.9. The composition of claim lwherein it retains at least 50% of its surface area after exposure to liquid water at 60° C. for 6 hours.10. The MOF of further characterized in that the MOF is formed into a shaped body selected from pellets claim 1 , spheres claim 1 , disks claim 1 , monolithic body claim 1 , irregularly shaped particles claim 1 , extrudates claim 1 , and ...

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

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

MODIFIED POROUS HYPERCROSSLINKED POLYMERS FOR CO2 CAPTURE AND CONVERSION

The present disclosure describes a process for making a hyperporous material for capture and conversion of carbon dioxide. The process comprises the steps a first self-polymerisation of benzyl halides via Friedel-Crafts reaction. In the second step the obtained hypercrosslinked polymer is further coupled with an amine or heterocyclic compound having at least one nitrogen ring atom. The invention also relates to the material obtained to the process and its use in catalytic reactions, for instance the conversion of epoxides to carbonates. Salt-modified porous hypercrosslinked polymers obtained according to the invention show a high BET surface (BET surface area up to 926 m/g) combined with strong COcapture capacities (14.5 wt %). The nitrogen compound functionalized hypercrosslinked polymer catalyst shows improved conversion rates compared to known functionalized polystyrene materials and an excellent recyclability. A new type of imidazolium salt modified polymers shows especially high capture and conversion abilities. Carbonates can be produced in high yields according to the inventive used of the obtained polymers. 1. A process for making a hypercrosslinked , porous polymer material comprising the steps of:(a) a self-polymerisation of benzyl halides via Friedel-Crafts reaction, and(b) coupling of an amine or heterocyclic compound having at least one nitrogen ring atom to the obtained polymer.2. The process of claim 1 , wherein the heterocyclic compound in step (b) is an optionally substituted heterocyclic compound having 5 or 6 ring atoms and 1 to 3 hetero atoms in the optionally benzofused ring and is coupled to the polymer to form a salt.3. The process of claim 2 , wherein the heterocyclic compound is an optionally benzofused claim 2 , optionally heteroaromatic fused and optionally C-C-alkyl claim 2 , halogen claim 2 , cyano or nitro substituted pyrrole claim 2 , pyrrolidine claim 2 , pyrroline claim 2 , piperidine claim 2 , imidazole claim 2 , imidazoline claim 2 ...

CATALYST, CATALYST CARRIER OR ABSORBENT MONOLITH OF STACKED STRANDS

A three-dimensional porous catalyst, catalyst carrier or absorbent monolith of stacked strands of catalyst, catalyst carrier or absorbent material, composed of alternating layers of linear spaced-apart parallel strands, wherein the strands in alternating layers are oriented at an angle to one another, wherein the distance between inner spaced-apart parallel strands is larger than the distance between outer spaced-apart parallel strands in at least a part of the layers of the monolith. 1. A three-dimensional porous catalyst , catalyst carrier or absorbent monolith of stacked strands of catalyst , catalyst carrier or absorbent material , composed of alternating layers of linear spaced-apart parallel strands , wherein the strands in alternating layers are oriented at an angle to one another , wherein the distance between inner spaced-apart parallel strands is larger than the distance between outer spaced-apart parallel strands in at least a part of the layers of the monolith.2. The monolith of claim 1 , wherein the strands are arranged in alternating layers comprising first and second alternate layers claim 1 , wherein the strands in the first alternate layers and in the second alternate layers are each aligned claim 1 , and wherein the strands in the alternate layers are orthogonal to one another.3. The monolith of claim 1 , wherein the strands are arranged in alternating layers comprising first claim 1 , second and third alternate layers claim 1 , wherein the strands in the first alternate layers claim 1 , in the second alternate and in the third alternate layers are each aligned claim 1 , and wherein the strands in the alternate layers are oriented at 60° and 120° claim 1 , respectively claim 1 , to one another.4. The monolith of claim 1 , wherein the strands are arranged in alternating layers comprising first claim 1 , second claim 1 , third and fourth alternate layers claim 1 , wherein the strands in the first alternate layers claim 1 , in the second alternate ...

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

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

HIGH GEOMETRIC SURFACE AREA CATALYSTS FOR VINYL ACETATE MONOMER PRODUCTION

A catalyst includes a support, where the support includes an external surface, about 60 wt % to about 99 wt % silica, and about 1.0 wt % to about 5.0 wt % alumina. A catalytic layer is disposed within the support adjacent to the external surface, where the catalytic layer further includes Pd, Au, and potassium acetate (KOAc). In the catalyst, (a) the KOAc is from about 60 kg/mto about 150 kg/mof the catalyst; or (b) the catalytic layer has an average thickness from about 50 μm to about 150 μm; or (c) both (a) and (b). The catalyst also possesses a Brunauer-Emmett-Teller surface area of about 130 m/g to about 300 m/g and a geometric surface area per packed bed volume from about 550 m/mto about 1500 m/m. The catalyst is highly active for the synthesis of vinyl acetate monomer and exhibits a high selectivity for vinyl acetate monomer. 1. A catalyst comprising: an external surface;', 'about 60 wt % to about 99 wt % silica; and', 'about 1.0 wt % to about 5.0 wt % alumina;, 'a support comprisinga catalytic layer disposed within the support adjacent to the external surface, where the catalytic layer further comprises Pd, Au, and potassium acetate (KOAc);{'sup': 2', '2, 'a Brunauer-Emmett-Teller surface area of about 130 m/g to about 300 m/g; and'}{'sup': 2', '3', '2', '3, 'a geometric surface area per packed bed volume from about 800 m/mto about 1300 m/m;'} [{'sup': 3', '3, '(a) the KOAc is from about 60 kg/mto about 150 kg/mof the catalyst; or'}, '(b) the catalytic layer has an average thickness from about 50 μm to about 150 μm, or', {'sup': 3', '3, '(c) the KOAc is from about 60 kg/mto about 150 kg/mof the catalyst and the catalytic layer has an average thickness from about 50 μm to about 150 μm.'}], 'wherein'}2. The catalyst of claim 1 , wherein the KOAc is from about 65 kg/mto about 100 kg/mof the catalyst.3. The catalyst of claim 1 , wherein the catalytic layer has an average thickness from about 100 μm to about 200 μm.4. The catalyst of claim 1 , wherein the alumina ...

Clean Gas Stack

A flow-through solid catalyst formed by coating a zeolite material on a metal or ceramic solid substrate. In some embodiments, the solid substrate is formed as flat plates, corrugated plates, or honeycomb blocks. 1. An apparatus for drying and cleaning stack gases from a fossil fuel source , the apparatus comprising: [{'sup': '2', 'a zeolite material with a porosity of a total surface area of not greater than 1200 m/g and effective for achieving at least 70% reduction in carbon oxides, sulfur oxides, or nitrogen oxides from the stack gases;'}, 'a metal or ceramic solid substrate to which the zeolite material has been applied to create a zeolite-coated solid substrate; and', 'spacing between components of the substrate being selected based on a flow-through capacity of, a pressure drop across, and an effectiveness of removal of carbon oxides, sulfur oxides, or nitrogen oxides by the flow-through solid catalyst; and, 'a plurality of flow-through solid catalysts, each of the plurality of flow-through solid catalysts comprisinga pair of electrodes positioned inline in a gas flow upstream of the plurality of flow-through solid catalysts, the electrodes being insulated from containment of the gas flow, with a DC voltage applied between the electrodes to ionize water vapor in the gas flow without creating substantial amounts of hydrogen gas and to reduce moisture content of the gas flow through the flow-through solid catalysts.2. The apparatus of claim 1 , the DC voltage applied between the electrodes being less than 34 volts.3. The apparatus of claim 1 , the solid substrate comprising a material selected from a group consisting of stainless steel claim 1 , copper claim 1 , titanium claim 1 , a titanium alloy claim 1 , aluminum claim 1 , cordierite claim 1 , mullite claim 1 , and alumina.4. The apparatus of claim 1 , each of the plurality of flow-through solid catalysts further comprising a binder to increase adherence of the zeolite material to the substrate.5. The ...

SILICA-TITANIA COMPOSITE AEROGEL PARTICLE, PHOTOCATALYST-FORMING COMPOSITION, AND PHOTOCATALYST

A silica-titania composite aerogel particle includes: a base particle including silicon and titanium whose element ratio Si/Ti is more than 0 and 6 or less; and a surface layer present on the base particle and including a metal compound having a metal atom and a hydrocarbon group. The silica-titania composite aerogel particle has absorption at wavelengths of 450 nm and 750 nm in a visible absorption spectrum, has a BET specific surface area in the range of 200 m/g to 1,200 m/g, and has a value A in the range of 0.03 to 0.3. The value A is calculated by formula: A=(peak intensity of C—O bond+peak intensity of C═O bond)/(peak intensity of C—C bond+peak intensity of C═C bond). The peak intensity is obtained from a C is XPS spectrum. 1. A silica-titania composite aerogel particle comprising:a base particle that includes silicon and titanium whose element ratio Si/Ti is more than 0 and 6 or less; anda surface layer that is present on the base particle and includes a metal compound having a metal atom and a hydrocarbon group,and the silica-titania composite aerogel particle has absorption at wavelengths of 450 nm and 750 nm in a visible absorption spectrum,{'sup': 2', '2, 'has a BET specific surface area in a range of 200 m/g to 1,200 m/g, and has a value A being calculated by formula below in a range of 0.03 to 0.3A=(peak intensity of C—O bond+peak intensity of C═O bond)/(peak intensity of C—C bond+peak intensity of C═C bond)wherein the peak intensity is a value obtained from a C is XPS spectrum.2. The silica-titania composite aerogel particle according to claim 1 , wherein the silica-titania composite aerogel particle has absorption over an entire wavelength range of 400 nm to 800 nm in the visible absorption spectrum.3. The silica-titania composite aerogel particle according to claim 1 , wherein the silica-titania composite aerogel particles have a volume average particle size in a range of 0.1 μm to 3 μm and a volume particle size distribution in a range of 1.5 to 10. ...

SILICA TITANIA COMPOSITE AEROGEL PARTICLE, PHOTOCATALYST FORMING COMPOSITION, AND PHOTOCATALYST

Provided is a silica titania composite aerogel particle including a base particle in which an element ratio Si/Ti of silicon to titanium is greater than 0 and equal to or lower than 6. A BET specific surface area of the silica titania composite particle is within a range of 200 m/g to 1200 m/g, and the silica titania composite particle has absorption at wavelengths of 450 nm and 750 nm. 1. A silica titania composite aerogel particle comprising:a base particle in which an element ratio Si/Ti of silicon to titanium is greater than 0 and equal to or lower than 6,{'sup': 2', '2, 'and a BET specific surface area of the silica titania composite aerogel particle is within a range of 200 m/g to 1200 m/g, and'}the silica titania composite aerogel particle has absorption at wavelengths of 450 nm and 750 nm.2. The silica titania composite aerogel particle according to claim 1 ,wherein the silica titania composite aerogel particle has absorption within a range of a wavelength of 400 nm to 800 nm.3. The silica titania composite aerogel particle according to claim 1 ,wherein the silica titania composite aerogel particles have a volume average particle diameter of 0.1 μm to 3 μm, and a volume particle size distribution in a range of 1.5 to 10.4. The silica titania composite aerogel particle according to claim 1 ,wherein the base particle is an aggregated particle in which primary particles are aggregated, andan average particle diameter of the primary particle is 1 nm to 90 nm.5. The silica titania composite aerogel particle according to claim 1 , comprising a first layer formed of titania on the base particle.6. The silica titania composite aerogel particle according to claim 5 , further comprising a second layer on the first layer claim 5 , the second layer containing a metallic compound having a metal atom and a hydrocarbon group.7. The silica titania composite aerogel particle according to claim 6 ,wherein the metallic compound of the second layer is bonded to the first layer ...

CATALYST FOR DEHYDROGENATION REACTION OF FORMATE AND HYDROGENATION REACTION OF BICARBONATE AND PREPARATION METHOD THEREOF

Provided is a method for preparing a catalyst for a dehydrogenation reaction of formate and a hydrogenation reaction of bicarbonate, the method including: adding a silica colloid to a polymerization step of polymerizing aniline and reacting the resulting mixture to form a poly(silica-aniline) composite; carbonizing the corresponding poly(silica-aniline) composite under an atmosphere of an inert gas; removing silica particles from the corresponding poly(silica-aniline) composite to form a polyaniline-based porous carbon support; and fixing palladium particles on the corresponding polyaniline-based porous carbon support to prepare the catalyst. 1. A method for preparing a catalyst for a dehydrogenation reaction of formate and a hydrogenation reaction of bicarbonate , the method comprising:adding a silica colloid to a polymerization step of polymerizing aniline to form polyaniline and reacting the resulting mixture to form a poly(silica-aniline) composite;carbonizing the poly(silica-aniline) composite under an atmosphere of an inert gas;removing silica particles from the poly(silica-aniline) composite to form a polyaniline-based porous carbon support; andfixing palladium particles on the polyaniline-based porous carbon support to prepare the catalyst.21. The method according to , wherein the catalyst is represented by the following Chemical Formula 1:{'br': None, 'Pd/PDMC-T-X\u2003\u2003[Chemical Formula 1]'}(In Chemical Formula 1, Pd and PDMC mean palladium and a polyaniline-based porous carbon support, respectively, T means a temperature in the carbonization step, and X is a weight (g) of the silica colloid added per 0.02 mmol of aniline in the polymerization step of polyaniline).32. The method according to , wherein T in Chemical Formula 1 is within a range of 500 to 1 ,000° C.43. The method according to , wherein T in Chemical Formula 1 is within a range of 750 to 860° C.52. The method according to , wherein X in Chemical Formula 1 is within a range of 4 to 18 g.65 ...

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

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

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

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

CATALYST

The Fischer-Tropsch process can be used for the conversion of hydrocarbonaceous feed stocks into normally liquid and/or solid hydrocarbons. The feed stock (e.g. natural gas, associated gas and/or coal-bed methane, coal) is converted in a first step into a mixture of hydrogen and carbon monoxide (this mixture is often referred to as synthesis gas or syngas). The synthesis gas (or syngas) is then converted in one or more steps over a suitable catalyst at elevated temperature and pressure into paraffinic compounds ranging from methane to high molecular weight molecules comprising up to 200 carbon atoms, or, under particular circumstances, even more. The present invention relates to a catalyst, a method for manufacturing said catalyst. The present invention further relates to a catalyst obtainable by said method. The present invention further relates to a multi tubular reactor comprising said catalyst. 1. A catalyst for carrying out a Fischer-Tropsch reaction comprising a matrix material (1) and a catalytic material (2) wherein the catalyst comprises stepped-shape channels through which synthesis gas comprising hydrogen and carbon monoxide can flow.2. A catalyst according to wherein the stepped-shape channels are stepped shaped such that a fluid flowing through the catalyst moves up/down a stairs.3. A catalyst according to wherein said channels are in connection with each other such that a fluid can flow from one channel to an adjacent channel.4. A catalyst according to wherein the catalyst has an open volume of more than 60% claim 1 , with respect to the reactor volume.5. A catalyst according to wherein the catalyst has a specific surface area from 1000-5000 m2/m3.6. A catalyst according to wherein the catalytic material is present as a layer on the channel wall and has a layer thickness of from about 1 to 300 microns.7. A catalyst according to wherein the catalytic material comprises a catalyst support material wherein the catalyst support material is selected from ...

Catalyst Carrier

A catalyst carrier may have a cross-sectional shape that may include a plurality of surface channels having a first channel width and a second channel width, where the first channel width may be closer to a periphery of the cross-sectional shape than the second channel width and the first channel width may be less than the second channel width. The cross-sectional shape may further include a plurality of surface features where at least one surface feature is located between at least one pair of surface channels. The cross-sectional shape may further include a ratio L/Lof at least about 1.7, where Lis a length of a total contour of the cross-sectional shape and Lis a length of an outer simple convex perimeter of the cross-sectional shape. 1. A catalyst carrier having a cross-sectional shape comprising:a plurality of surface channels, each surface channel having a first channel width and a second channel width, wherein the first channel width is closer to a periphery of the cross-sectional shape than the second channel width and wherein the first channel width is less than the second channel width;a plurality of surface features, wherein at least one surface feature is located between at least one pair of adjacent surface channels; and{'sub': OC', 'SCP', 'OC', 'SCP, 'a ratio L/Lof at least about 1.7, where Lis a length of a total contour of the cross-sectional shape and Lis a length of an outer simple convex perimeter of the cross-sectional shape.'}2. The catalyst carrier claim 1 , wherein the cross-sectional shape further comprises a ratio L/Lof not greater than about 2.8.3. The catalyst carrier of claim 1 , wherein the catalyst carrier further comprises a ratio GSA/dP of at least about 0.62 (m/m)/(Pa/m) and not greater than about 0.98 claim 1 , where GSA is a geometric surface area of the catalyst carrier and dP is a pressure drop of the catalyst carrier as measured at a mass flow of 2440 kg/mhr (500 lbs/ft*hr).4. The catalyst carrier of claim 1 , wherein the ...

SULFUR-DOPED CARBONACEOUS POROUS MATERIALS

The present invention relates to novel sulfur-doped carbonaceous porous materials. The present invention also relates to processes for the preparation of these materials and to the use of these materials in applications such as gas adsorption, mercury and gold capture, gas storage and as catalysts or catalyst supports. 1. A process for the preparation of a sulfur-doped carbonaceous porous material , the process comprising the steps of:i) preparing a sulfur-based polymer by reacting elemental sulfur with one or more organic crosslinking agents, wherein the organic crosslinking agent(s) comprises two or more carbon-carbon double bonds;ii) carbonising the sulfur-based polymer of step (i) in the presence of at least one porosity enhancement agent.2. A process according to claim 1 , wherein the sulfur-doped carbonaceous porous material comprises greater than or equal to 5 wt % sulfur.3. A process according to claim 1 , wherein the sulfur-doped carbonaceous porous material comprises greater than or equal to 10 wt % sulfur.4. A process according to any one of to claim 1 , wherein the porosity enhancement agent is an inorganic base claim 1 , an inorganic acid or an inorganic salt.5. A process according to any one of to claim 1 , wherein the porosity enhancement agent is selected from potassium hydroxide claim 1 , phosphoric acid claim 1 , sodium hydroxide claim 1 , calcium chloride claim 1 , magnesium chloride claim 1 , or zinc chloride.6. A process according to any one of to claim 1 , wherein the porosity enhancement agent is an inorganic base (e.g. potassium hydroxide).7. A process according to any one of to claim 1 , wherein the carbonisation of step (ii) is conducted at a temperature of between 500° C. and 1000° C.8. A process according to any one of to claim 1 , wherein the carbonisation of step (ii) is conducted at a temperature of between 650° C. and 850° C.9. A process according to any one of to claim 1 , wherein the mass ratio of sulfur-based polymer to porosity ...

FLUID PROCESSING IN ENCAPSULATED POROUS STRUCTURES

A porous material structure and device are described and shown to enhance the mass transfer and/or heat transfer at low pressure drops for removal of certain molecular species from a fluid by adsorption and/or catalytic reaction. The porous structure of active materials comprising packed fine particles of adsorbents or catalysts is encapsulated with a thin membrane to provide large interfacing area with the fluid per unit volume for rapid mass transfer between the porous structure and fluid. The thin membrane also blocks particulate from getting into the porous structure of the active material. For the process involving significant heat of adsorption and/or reaction, the another surface of the porous structure of the active material is encapsulated with a thin non-permeable sheet to interface with a thermal fluid for rapid heat transfer between the porous structure and the thermal fluid. The device can be used for removal of CO, moisture, and hydrocarbon molecules from a gas stream with rapid in-situ regeneration. The device can be used for removal of water from water-containing liquid fluids, such as solvents and oils. The device can be used for removal of bacteria, virus, salts, and molecular contaminants from one water simultaneously. 1. A filter for processing fluid , the filter comprising:a porous structure including one or more chemically active materials; and the thickness of the volume is less than the length of the volume,', 'the first sheet is fluid permeable,', 'the porous structure spans each dimension of the volume, and', 'in a direction perpendicular to the length of the volume, compressive strength of the frame alone is greater than compressive strength of the porous structure alone., 'a frame including a first sheet, a second sheet, and a seal collectively defining a volume, the volume having a thickness between the first sheet and the second sheet and a length parallel to the first sheet and the second sheet, wherein'}2. The filter of claim 1 , ...

HIGH GEOMETRIC SURFACE AREA CATALYSTS FOR VINYL ACETATE MONOMER PRODUCTION

A catalyst includes a support, where the support includes an external surface, about 60 wt % to about 99 wt % silica, and about 1.0 wt % to about 5.0 wt % alumina. A catalytic layer is disposed within the support adjacent to the external surface, where the catalytic layer further includes Pd, Au, and potassium acetate (KOAc). In the catalyst, (a) the KOAc is from about 60 kg/mto about 150 kg/mof the catalyst; or (b) the catalytic layer has an average thickness from about 50 μm to about 150 μm; or (c) both (a) and (b). The catalyst also possesses a Brunauer-Emmett-Teller surface area of about 130 m/g to about 300 m/g and a geometric surface area per packed bed volume from about 550 m/mto about 1500 m/m. The catalyst is highly active for the synthesis of vinyl acetate monomer and exhibits a high selectivity for vinyl acetate monomer. 1. A catalyst comprising: an external surface;', 'about 60 wt % to about 99 wt % silica; and', 'about 1.0 wt % to about 5.0 wt % alumina;, 'a support comprisinga catalytic layer disposed within the support adjacent to the external surface, where the catalytic layer further comprises Pd, Au, and potassium acetate (KOAc);{'sup': 2', '2, 'a Brunauer-Emmett-Teller surface area of about 130 m/g to about 300 m/g; and'}{'sup': 2', '3', '2', '3, 'a geometric surface area per packed bed volume from about 550 m/mto about 1500 m/m;'}wherein a void fraction of the catalyst is from about 35% to about 55%; and [{'sup': 3', '3, '(a) the KOAc is from about 60 kg/mto about 150 kg/mof the catalyst; or'}, '(b) the catalytic layer has an average thickness from about 50 μm to about 150 μm, or', {'sup': 3', '3, '(c) the KOAc is from about 60 kg/mto about 150 kg/mof the catalyst and the catalytic layer has an average thickness from about 50 μm to about 150 μm.'}], 'wherein;'}2. The catalyst of claim 1 , wherein the KOAc is from about 65 kg/mto about 100 kg/mof the catalyst.3. The catalyst of claim 1 , wherein the alumina is present in the catalyst from about 1. ...

CARBIDE-DERIVED CARBONS HAVING INCORPORATED METAL CHLORIDE OR METALLIC NANOPARTICLES

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

PT AND/OR PD EGG-SHELL CATALYST AND USE THEREOF

The present invention is in the field of catalysis. More particularly, the present invention is directed to supported precious metal catalysts, preferably palladium and/or platinum metal catalysts, having a high metal loading, a high degree of dispersion and a high degree of edge-coating. The present invention is further directed to a process for producing these catalysts, as well as to the use of these catalysts in chemical reactions. 1. A precious metal catalyst , wherein said catalyst comprises nanocrystallites of precious metal on a powder support , wherein the nanocrystallites have an average size of from 1 to less than 5 nm , wherein the catalyst comprises precious metal in an amount of at least 1.0 wt. % , based on the weight of the catalyst , and wherein the precious metal is palladium and/or platinum metal; and ,wherein the palladium metal catalyst has a surface enrichment value of from at least 6.5 to at most 150; and,wherein the platinum metal catalyst has a surface enrichment value of from at least 1.5 to at most 150, and, {'br': None, 'SEV=(XPS wt. %×ICP wt. %)/ICP wt. %;\u2003\u2003(I)'}, 'wherein the surface enrichment value (SEV) is determined from the following formula (I)wherein XPS wt. % is the X-ray photoelectron spectroscopy (XPS) measurement and ICP wt. % is the inductively coupled plasma (ICP) measurement of the precious metal content in weight percent of said catalyst.2. The catalyst according to claim 1 ,wherein the palladium metal catalyst has a surface enrichment value of at least 8; and, wherein the palladium metal catalyst has a surface enrichment value of at most 120; and,wherein the platinum metal catalyst has a surface enrichment value of at least 2; and, wherein the platinum metal catalyst has a surface enrichment value of at most 120.3. The catalyst according to claim 1 , wherein the catalyst comprises palladium and/or platinum metal in an amount of between more than 1.0 wt. % and 20 wt. % claim 1 , based on the weight of the ...

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

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

Catalyst Carrier

A catalyst carrier may have a cross-sectional shape that may include a plurality of surface channels having a first channel width and a second channel width, where the first channel width may be closer to a periphery of the cross-sectional shape than the second channel width and the first channel width may be less than the second channel width. The cross-sectional shape may further include a plurality of surface features where at least one surface feature is located between at least one pair of surface channels. The cross-sectional shape may further include a ratio L/Lof at least about 1.7, where Lis a length of a total contour of the cross-sectional shape and Lis a length of an outer simple convex perimeter of the cross-sectional shape. 1. A catalyst carrier having a cross-sectional shape comprising:a plurality of surface channels, each surface channel having a first channel width and a second channel width, wherein the first channel width is closer to a periphery of the cross-sectional shape than the second channel width and wherein the first channel width is less than the second channel width;a plurality of surface features, wherein at least one surface feature is located between at least one pair of adjacent surface channels; and{'sup': 2', '3', '2', '2, 'wherein the catalyst carrier comprises a ratio GSA/dP of at least about 0.62 (m/m)/(Pa/m), where GSA is a geometric surface area of the catalyst carrier and dP is a pressure drop of the catalyst carrier as measured at a mass flow of 2440 kg/m*hr (500 lbs/ft*hr).'}2. The catalyst carrier of claim 1 , wherein the catalyst carrier further comprises a ratio GSA/PCof not greater than about 0.98.3. The catalyst carrier of claim 1 , wherein the catalyst carrier further comprises a ratio GSA/PCof at least about 5.9 claim 1 , where GSA is the geometric surface area of the catalyst carrier and PC is a calculated piece count.4. The catalyst carrier of claim 1 , wherein the catalyst carrier further comprises a GSA at least ...

MESOPOROUS AND MACROPOROUS CATALYST FOR HYDROCONVERSION OF RESIDUES AND PREPARATION METHOD

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

METHOD FOR PREPARATION OF SIZE-MODULATED UIO-66 AND CATALYST FOR HYDROLYSIS OF CHEMICAL WARFARE AGENTS WITH ENHANCED ACTIVITY PREPARED THEREBY

The present invention relates to a method for preparing size-modulated UiO-66, which is achieved by modulating the concentrations of reactants, and a catalyst with improved activity of hydrolyzing chemical warfare agents prepared by the method. 1. A method for preparing size-modulated UiO-66 , comprising:{'sub': '4', 'a first step of preparing a first solution comprising ZrClat a concentration of 0.15 M to 0.5 M;'}a second step of preparing a second solution comprising terephthalic acid (benzene-1,4-dicarboxylic acid; BDC) at a concentration of 0.1 M to 0.5 M; anda third step of mixing the first solution and the second solution in a ratio of 1:1 to 1:3 to react,{'sub': '4', 'wherein the first solution comprises hydrochloric acid in an amount of 8 to 15 moles per mole of ZrCl.'}2. The method of claim 1 , wherein both the first solution and the second solution are prepared using N claim 1 ,N-dimethylformamide (DMF) as a solvent.3. The method of claim 1 , wherein the third step is performed at 60° C. to 120° C. for 12 to 48 hours.4. The method of claim 1 , wherein particles of the ultimately prepared UiO-66 have an average diameter of 50 nm to 400 nm.5. The method of claim 1 , wherein the particle size of the ultimately prepared UiO-66 decreases as the concentrations of ZrCland terephthalic acid claim 1 , which are to be reacted claim 1 , increase.6. The method of claim 1 , wherein particles of the ultimately prepared UiO-66 have 1.65 to 1.9 missing linker sites on average within a single cluster.7. The method of claim 1 , wherein particles of the ultimately prepared UiO-66 have a specific surface area of 1400 m/g to 1500 m/g.8. The method of claim 1 , wherein particles of the ultimately prepared UiO-66 have an activity as a catalyst which hydrolyzes chemical warfare agents.9. A method for detoxifying chemical warfare agents (CWA) at a conversion rate of at least 50% within one minute claim 1 , comprising:a first step of adding a solution comprising a base and a ...

METAL ORGANIC FRAMEWORKS FOR THE CATALYTIC DETOXIFICATION OF CHEMICAL WARFARE NERVE AGENTS

A method of using a metal organic framework (MOF) comprising a metal ion and an at least bidendate organic ligand to catalytically detoxify chemical warfare nerve agents including exposing the metal-organic-framework (MOF) to the chemical warfare nerve agent and catalytically decomposing the nerve agent with the MOF. 1. A method of using a metal organic framework (MOF) comprising a metal ion and an at least bidendate organic ligand to catalytically detoxify chemical warfare nerve agents comprising:exposing the MOF to the chemical warfare nerve agent; andcatalytically decomposing the nerve agent with the MOF, {'sub': x', 'y', 'z', '3', 'r, 'TiZrHf(μ-O), where x+y+z=6 and r=4, 6 or 8.'}, 'wherein metal nodes of the MOF comprise derivatives of2. The method of claim 1 , wherein the metal nodes of the MOF comprise: TiZrHf(μ-O)(A)(B)(C)(D)(E)(F) claim 1 , wherein A=(μ-OH) claim 1 , B=(HO) claim 1 , C=(OH) claim 1 , D=(O) claim 1 , E=X claim 1 , F=(RCOO) claim 1 , wherein a+b+c+d+e+f≧2 and each of a claim 1 , b claim 1 , c claim 1 , d claim 1 , e and f=0 or 1.3. The method of claim 1 , [{'sub': x', 'y', 'z', '3', '4', '3', '4', '2', '6', '6', '2', '6', 'x', 'y', 'z', '3', '8', '2', '6, 'TiZrHf(μ-O)(μ-OH)(HO)(OH)(O)or TiZrHf(μ-O)(O)and where the oxygen atoms from the organic linker are included in the formula and where x+y+z=6; or'}, {'sub': x', 'y', 'z', '3', '4', '3', 'l', 'm', 'L', '24', 'L, 'TiZrHf(μ-O)(μ-OH)X(O)where x+y+z=6, m=0-8 O=any carboxylate oxygen atoms on a mono-, di-, -, or tetra-dentate ligand, and l+m=4; where X is any anion with a −1 charge; or'}, {'sub': x', 'y', 'z', '3', '4', '3', '4', 'l', 'm', '2', 'n', 'L', '16', 'L, 'TiZrHf(μ-O)(μ-OH)(OH)X(HO)(O)where x+y+z=6 n=0-8, O=any carboxylate oxygen atoms on a mono-, tri-, or tetra-dentate ligand, and l+m=4; where X is any anion with a −1 charge; or'}, {'sub': x', 'y', 'z', '3', '4', '3', 'l', 'm', '6', 'L', '12', 'L, 'TiZrHf(μ-O)(μ-OH)X(RCOO)(O)where x+y+z=6, O=any carboxylate oxygen atoms on a mono-, di-, ...

SULFUR DIOXIDE REMOVAL FROM WASTE GAS

A process where a gas, containing SOand Ois brought in contact with a mixture of from 95% vol. to 50% vol. of activated carbon catalyst and from 5% vol. to 50% vol. of an inert filler material, where the SOis converted to HSOon the activated carbon catalyst and is then washed from the activated carbon catalyst to obtain a HSOsolution. 1. A process , comprising:{'sub': 2', '2, 'bringing a gas, containing SOand Ois brought, in contact with a mixture of from 95% vol. to 50% vol. of activated carbon catalyst and from 5% vol. to 50% vol. of an inert filler material;'}wherein the mixture is a mixture of separate, distinct particles of filler and separate, distinct particles of activated carbon catalyst; and{'sub': 2', '2', '4', '2', '4, 'wherein the SOis converted to HSOon the activated carbon catalyst and is then washed from the activated carbon catalyst to obtain a HSOsolution.'}2. The process as claimed in claim 1 , wherein the filler material is between 10% vol. and 30% vol. of the mixture of activated carbon catalyst and a filler material.3. The process as claimed in claim 1 , wherein the mixture contains no other solid ingredients than the activated carbon catalyst and the filler material.4. The process as claimed in claim 1 , wherein the activated carbon catalyst is chosen from impregnated or activated carbon catalysts.5. The process as claimed in claim 1 , wherein the filler is chosen from fillers made of ceramic material claim 1 , made of metal claim 1 , fillers made of plastic mineral or mixtures thereof.6. The process as claimed in claim 1 , wherein the filler material is a shape comprising saddle shaped claim 1 , ring shaped claim 1 , ball shaped claim 1 , torus shaped claim 1 , prism shaped or irregular shaped.7. The process as claimed in claim 1 , wherein the mixture is in a fixed bed.8. The process as claimed in claim 1 , wherein the mixture is washed with water or an aqueous solution in an amount between 5 l/hour/mof catalyst and 100 l/hour/mof mixture.9. ...

RUTHENIUM-BASED CATALYST FOR AMMONIA AYNTHESIS AND PREPARATION METHOD AND USE THEREOF

Disclosed is a ruthenium-based catalyst for ammonia synthesis, preparation method and use thereof. The ruthenium-based catalyst comprises Ru—Ba-A core-shell structure which comprises a ruthenium nanoparticle as a core covered with a first shell and a second shell sequentially, wherein the first shell consists of a barium nanoparticle, and the second shell consists of a metal oxide. The Ru—Ba-A core-shell structure can effectively preventing agglomerations of ruthenium nanoparticles during the use of the catalyst and avoiding direct contact between the ruthenium nanoparticles and the metal oxides. In addition, barium nanoparticles have a promoting effect as an electronic promoter, which can effectively improve the stability and catalytic activity of ruthenium-based catalyst for ammonia synthesis, especially in the system for synthesizing ammonia from a coal gas. 1. A ruthenium-based catalyst for ammonia synthesis , comprising Ru—Ba-A core-shell structure , the Ru—Ba-A core-shell structure comprising a ruthenium nanoparticle as a core which is covered with a first shell and a second shell sequentially , wherein the first shell consists of a barium nanoparticle , and the second shell consists of a metal oxide.2. The ruthenium-based catalyst of claim 1 , further comprising a composite support which comprises a support member having an electron promoter dispersed on a surface of the support member claim 1 , and the Ru—Ba-A core-shell structure being supported on the composite support.3. The ruthenium-based catalyst of claim 2 , wherein based on mass of the support member claim 2 , the ruthenium nanoparticle accounts for 3 wt. % to 5 wt. % claim 2 , metal ions in the barium nanoparticle and metal oxide account for 3 wt. % to 20 wt. % claim 2 , and metal ions in the electron promoter account for 3 wt. % to 20 wt. %.4. The ruthenium-based catalyst of claim 3 , wherein the support member is a graphitized activated carbon support; and the electron promoter is an oxide of an ...

CATALYST FOR HIGH TEMPERATURE STEAM REFORMING

This invention relates to highly active and stable catalyst composite used in high temperature synthesis gas production. More specifically, nickel alumina catalysts doped with noble metals and lanthanide groups or transition metal groups containing a lattice spinel structure with a general formula [NiA] [(BAl)]OStabilizers such as yttria-stabilized zirconia are also integrated in this composite to enhance high temperature catalytic performance. The catalyst composite of present invention exhibits high redox tolerance, coking resistance, high temperature stability, and high catalytic activity. 2. The catalyst of claim 1 , wherein the second metal dopant (B) is part of the spinel lattice structure as indicated by the absence of the XRD peak corresponding to the oxide of the second metal dopant.3. The catalyst of claim 1 , wherein the second metal dopant (B) is Ce claim 1 , and the peak intensity ratio of I(2-theta of 28.7°) to I(2-theta of 37.2°) is less than 0.9.4. The catalyst of claim 1 , wherein the active metal Ni is part of the spinel lattice structure of formula I and the peak intensity ratio of the Bragg's angle 2-theta of 37.2° to the Bragg's angle 2-theta of 65.7° is less than 2.0.5. The catalyst claim 1 , wherein said second metal dopant B is selected from the group consisting of La claim 1 , Ce claim 1 , Ti claim 1 , V claim 1 , Cr claim 1 , Mn claim 1 , Fe claim 1 , Co claim 1 , Cu claim 1 , Y claim 1 , Zr and mixtures thereof.6. The catalyst of claim 5 , wherein said second metal dopant is derived from one or more of water soluble metal salts in form of a nitrate claim 5 , chloride claim 5 , acetate claim 5 , oxalate claim 5 , halide claim 5 , sulfate and/or a hydrate thereof.7. The catalyst of claim 5 , wherein the first metal dopant (A) is Pt claim 5 , Rh claim 5 , and/or Ru and the second metal dopant (B) is Ce.8. The catalyst of claim 1 , wherein the Ni is present in an amount of about 5 wt % to about 33 wt % based on a total weight of the catalyst.9 ...

CATALYST AND METHOD FOR PRODUCING DIENE COMPOUND

A catalyst includes at least one element X selected from the group consisting of Groups 3 to 6 of the Periodic Table, and at least one element Z selected from the group consisting of Group 14 elements. At least one diffraction peak is observed in a low angle range of θ=6° or less in an X-ray diffraction profile observed using X-ray diffraction. The at least one diffraction peak has a ratio (I/H) of a peak intensity I to a half width at half maximum H of the diffraction peak of 5000 or more. 1. A catalyst comprising:at least one element X selected from the group consisting of Groups 3 to 6 of the Periodic Table; andat least one element Z selected from the group consisting of Group 14 elements, whereinat least one diffraction peak is observed in a low angle range of θ=6° or less in an X-ray diffraction profile observed using X-ray diffraction, andthe at least one diffraction peak has a ratio (I/H) of a peak intensity I to a half width at half maximum H of the diffraction peak of 5000 or more.2. The catalyst according to claim 1 , wherein a molar content (X/(X+Z)×100) of the element X with respect to the total amount (mole) of the element X and the element Z is 0.5 to 6 mol %.3. The catalyst according to claim 1 , wherein the element X is Hf and the element Z is Si.4. The catalyst according to claim 1 , wherein the catalyst is a diene compound synthesis catalyst for synthesizing a diene compound from a raw material including an alcohol.5. The catalyst according to claim 4 , wherein the raw material includes ethanol and/or acetaldehyde.6. The catalyst according to claim 1 , wherein a BET specific surface area is 700 to 1200 m/g and an average pore size is 2 to 20 nm.7. The catalyst according to claim 1 , wherein at least one diffraction peak having a half width at half maximum of 1° or more is observed in a high angle range of θ=10° to 40° in an X-ray diffraction profile observed using X-ray diffraction.8. A method for producing a diene compound claim 1 , comprising ...

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

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

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

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

SELECTIVE PARTIAL HYDROGENATION OF TERPENES USING AN IRIDIUM-BASED CATALYST

A process for selective partial hydrogenation of conjugated diene compounds includes at least one, preferably terminal, diene function and at least one additional carbon-carbon double bond, the process including reacting the conjugated diene compounds with hydrogen in the presence of an iridium-NHC based catalyst. The disclosure also relates to a reaction mixture that can be obtained at the end of the process. The disclosure also relates to the use of the reaction mixture. 1. A process for partial hydrogenation of conjugated diene compounds comprising at least one conjugated diene function and at least one additional carbon-carbon double bond , the process comprising reacting the conjugated diene compounds with hydrogen in the presence of an Iridium-NHC based catalyst , to produce a reaction mixture comprising partially hydrogenated compounds.2. The process according to claim 1 , wherein the at least one conjugated diene function is a terminal conjugated diene function.3. The process according to claim 1 , wherein a portion of the partially hydrogenated compounds results from mono-hydrogenation of one carbon-carbon double bond of the conjugated diene function.4. The process according to claim 1 , wherein a portion of the partially hydrogenated compounds results from di-hydrogenation of two carbon-carbon double bonds of the conjugated diene function.5. The process according to claim 1 , wherein the conjugated diene compounds comprising at least one conjugated diene function and at least one additional carbon-carbon double bond are selected from terpenes.6. The process according to claim 1 , wherein the hydrogenation is performed at a temperature ranging from 10° C. to 120 ° C.7. The process according to claim 1 , wherein the hydrogenation is performed at a pressure ranging from 2 bars to 12 bars.8. The process according to claim 1 , wherein the reaction mixture comprises mono-hydrogenated compounds wherein a mono-hydrogenated compound resulting from the hydrogenation ...

METHODS OF PRODUCING ORGANOSILICA MATERIALS AND USES THEREOF

Methods of preparing organosilica materials, which is a polymer comprising independent siloxane units of Formula [ZZSiCH](I), wherein each Zrepresents a hydroxyl group, a C-Calkoxy group or an oxygen atom bonded to a silicon atom of another siloxane unit and each Zrepresents a hydroxyl group, a C-Calkoxy group, a C-Calkyl group, or an oxygen atom bonded to a silicon atom of another siloxane, in the absence of a structure directing agent and/or porogen are provided herein. Processes of using the organosilica materials, e.g., for gas separation, etc., are also provided herein. 1. A method for preparing an organosilica material , the method comprising:(a) providing an aqueous mixture that contains essentially no structure directing agent and/or porogen,{'sup': 1', '2', '1', '2, 'sub': 2', '3', '1', '4', '1', '4', '1', '4, '(b) adding at least one compound of Formula [ZZSiCH](Ia) into the aqueous mixture to form a solution, wherein each Zrepresents a C-Calkoxy group and each Zrepresents a C-Calkoxy group or a C-Calkyl group;'}(c) aging the solution to produce a pre-product; and{'sup': 3', '4', '3', '4, 'sub': 2', '3', '1', '4', '1', '4', '1', '4, '(d) drying the pre-product to obtain an organosilica material which is a polymer comprising independent siloxane units of Formula [ZZSiCH](I), wherein each Zrepresents a hydroxyl group, a C-Calkoxy group or an oxygen atom bonded to a silicon atom of another siloxane unit and each Zrepresents a hydroxyl group, a C-Calkoxy group, a C-Calkyl group, or an oxygen atom bonded to a silicon atom of another siloxane.'}2. The method of claim 1 , wherein each Zrepresents a C-Calkoxy group.3. The method of claim 1 , wherein each Zrepresents a C-Calkoxy group.4. The method of claim 1 , wherein each Zrepresents a C-Calkoxy group.5. The method of claim 1 , wherein the at least one compound of Formula (Ia) is 1 claim 1 ,1 claim 1 ,3 claim 1 ,3 claim 1 ,5 claim 1 ,5-hexaethoxy-1 claim 1 ,3 claim 1 ,5-trisilacyclohexane.6. The method of claim 1 ...

ORGANOSILICA MATERIALS AND USES THEREOF

Organosilica materials, which are a polymer of at least one independent monomer of Formula [ZOZSiCH](I), wherein each Zrepresents a hydrogen atom, a C-Calkyl group or a bond to a silicon atom of another monomer and each Zrepresents a hydroxyl group, a C-Calkoxy group, a C-Calkyl group or an oxygen atom bonded to a silicon atom of another monomer and at least one other monomer are provided herein. Processes of using the organosilica materials, e.g., gas separation, etc., are also provided herein. 1. An organosilica material , which is a polymer of at least one independent monomer of Formula [ZOZSiCH](I) , wherein each Zrepresents a hydrogen atom , a C-Calkyl group or a bond to a silicon atom of another monomer and each Zrepresents a hydroxyl group , a C-Calkoxy group , a C-Calkyl group or an oxygen atom bonded to a silicon atom of another monomer and at least one other monomer selected from the group consisting of:{'sup': 3', '4', '5', '6', '3', '4', '5', '6, 'sub': 1', '4', '1', '4', '1', '4, '(i) an independent unit of formula ZOZZZSi (II), wherein each Zrepresents a hydrogen atom or a C-Calkyl group or a bond to a silicon atom of another monomer; and Z, Zand Zare each independently selected from the group consisting of a hydroxyl group, a C-Calkyl group, a C-Calkoxy group, and an oxygen atom bonded to a silicon atom of another monomer;'}{'sup': 7', '8', '9', '7', '8', '9', '7', '8', '9, 'sub': 1', '4, '(ii) an independent unit of formula ZZZSi—R—SiZZZ(III), wherein each Zindependently represents a hydroxyl group, a C-Calkoxy group or an oxygen atom bonded to a silicon atom of another comonomer; each Zand Zindependently represent a hydroxyl group,'}{'sub': 1', '4', '1', '4', '1', '8', '2', '8', '2', '8', '6', '20', '4', '20, 'a C-Calkoxy group, a C-Calkyl group or an oxygen atom bonded to a silicon atom of another monomer; and each R is selected from the group consisting a C-Calkylene group, a C-Calkenylene group, a C-Calkynylene group, an optionally substituted C- ...

ORGANOSILICA MATERIALS AND USES THEREOF

Provided herein are organosilica materials, which is a polymer of at least one monomer of Formula [ZOZOSiCH](I), wherein each Zand Zindependently represent a hydrogen atom, a C-Calkyl group or a bond to a silicon atom of another monomer. Processes of using the organosilica materials, e.g., for gas separation, are also provided herein. 1. An organosilica material , which is a polymer of at least one monomer of Formula [ZOZOSiCH](I) , wherein each Zand Zindependently represent a hydrogen atom , a C-Calkyl group or a bond to a silicon atom of another monomer , wherein the organosilica material exhibits an XRD pattern with only one peak , said peak being between about 1 and about 2 degrees 2θ , and wherein the organosilica material has an average pore diameter between about 2.5 nm and about 4 nm.2. The organosilica material of claim 1 , wherein each Zand Zindependently represent a hydrogen atom claim 1 , a C-Calkyl group or a bond to a silicon atom of another monomer.3. The organosilica material of claim 1 , wherein each Zand Zindependently represent a hydrogen atom claim 1 , ethyl or a bond to a silicon atom of another monomer.4. The organosilica material of further comprising at least one independent monomer of Formula [ZOZSiCH](II) claim 1 , wherein each Zrepresents a hydrogen atom claim 1 , a C-Calkyl group or a bond to a silicon atom of another monomer and each Zrepresents a C-Calkyl group.5. The organosilica material of claim 4 , wherein each Zrepresents a hydrogen atom claim 4 , a C-Calkyl group or a bond to a silicon atom of another monomer and each Zrepresents a C-Calkyl group.6. The organosilica material of claim 5 , wherein each Zrepresents a hydrogen atom claim 5 , ethyl or a bond to a silicon atom of another monomer and each Zrepresents methyl.7. The organosilica material of claim 1 , wherein the organosilica material has a total surface area of about 1000 m/g to about 2000 m/g.8. The organosilica material of claim 1 , wherein the organosilica material has ...

ORGANOSILICA MATERIALS AND USES THEREOF

Organosilica materials, which are a polymer of at least one independent monomer of Formula [ZOZOSiCH](I), wherein Zand Zeach independently represent a hydrogen atom, a C-Calkyl group or a bond to a silicon atom of another monomer and at least one other monomer is provided herein. Methods of preparing and processes of using the organosilica materials, e.g., for gas separation, color removal etc., are also provided herein. 1. An organosilica material , which is a polymer of at least one independent monomer of Formula [ZOZOSiCH](I) , wherein Zand Zeach independently represent a hydrogen atom , a C-Calkyl group or a bond to a silicon atom of another monomer and at least one other monomer selected from the group consisting of:{'sup': 3', '4', '5', '6', '3', '4', '5', '6, 'sub': 1', '4', '1', '4', '1', '4', '1', '10, '(i) an independent unit of Formula ZOZZZ(II), wherein each Zrepresents a hydrogen atom, a C-Calkyl group or a bond to a silicon atom of another monomer; and Z, Zand Zare each independently selected from the group consisting of a hydroxyl group, a C-Calkyl group, a C-Calkoxy group, a nitrogen-containing C-Calkyl group, a nitrogen-containing heteroaralkyl group, a nitrogen-containing optionally substituted heterocycloalkyl group, and an oxygen atom bonded to a silicon atom of another monomer;'}{'sup': 7', '8', '9', '1', '7', '8', '9', '7', '8', '9', '1, 'sub': 1', '4', '1', '4', '1', '4', '2', '10, '(ii) an independent unit of Formula ZZZSi—R—SiZZZ(III), wherein each Zindependently represents a hydroxyl group, a C-Calkoxy group or an oxygen bonded to a silicon atom of another comonomer; each Zand Zindependently represent a hydroxyl group, a C-Calkoxy group, a C-Calkyl group or an oxygen bonded to a silicon atom of another monomer; and each Rrepresents a nitrogen-containing C-Calkylene group; and'}(iii) a combination thereof.2. The organosilica material of claim 1 , wherein Zand Zeach independently represent a hydrogen atom claim 1 , a C-Calkyl group or a bond ...

METAL ORGANIC FRAMEWORKS FOR THE CATALYTIC DETOXIFICATION OF CHEMICAL WARFARE NERVE AGENTS

A method of using a metal organic framework (MOF) comprising a metal ion and an at least bidendate organic ligand to catalytically detoxify chemical warfare nerve agents including exposing the metal-organic-framework (MOF) to the chemical warfare nerve agent and catalytically decomposing the nerve agent with the MOF. 1. A metal-organic framework (MOF) comprising the coordination product of a metal ion and at least bidentate organic ligand , wherein the metal ion and the organic ligand are selected to assemble a MOF configured to catalytically detoxify chemical warfare nerve agents.2. The metal-organic framework of claim 1 , wherein the rate of catalytic detoxification comprises a measured catalytic half-life of no greater than 45 min measured at pH 10 with chemical warfare nerve agent concentration of 0.025 mol/L claim 1 , containing 6 mol % of catalyst claim 1 , and at 298 K.3. The metal-organic framework of claim 1 , wherein the MOF acts as a catalyst to detoxify the chemical warfare nerve agents and acts as a sorbent that selectively adsorbs the chemical warfare nerve agents.4. The metal-organic framework of claim 1 , wherein the MOF contains at least one bridging hydroxyl group.5. The metal-organic framework of claim 4 , wherein an oxygen atom of the at least one bridging hydroxyl group is connected to two atoms selected from the group consisting of titanium claim 4 , zirconium claim 4 , hafnium and combinations thereof.6. The metal-organic framework of claim 1 , wherein the MOF contains at least one terminal hydroxyl group or at least one terminal water molecule on a metal node.7. The metal-organic framework of claim 6 , wherein the terminal hydroxyl group or the terminal water molecule is connected to a metal cluster selected from the group consisting of titanium claim 6 , zirconium claim 6 , hafnium claim 6 , and combinations thereof.8. The metal-organic framework of claim 1 , wherein the MOF contains bridging oxo groups.9. The metal-organic framework of ...

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 ...

DEVICE AND CATALYST FOR USE WITH SAME

A device includes: a storage section which stores a solution containing an organic compound; a catalyst holding section to hold a solid catalyst; and a microwave irradiation mechanism which irradiates the solution passing through the catalyst holding section with a microwave, wherein the solid catalyst is a molded catalyst containing a noble metal supported on a carrier that has an average particle diameter larger than 100 μm. A hydrogen production method includes irradiating a solution containing an organic compound, the solution passing through a catalyst holding section holding a solid catalyst, with a microwave, the solid catalyst being a molded catalyst containing a noble metal supported on a carrier that has an average particle diameter larger than 100 μm. Both device and method do not require a high-temperature heat source, enable easy collection, replacement, of the catalyst, and can be used for production of hydrogen. 2. The device according to claim 1 , wherein the carrier comprises carbon.3. The device according to claim 1 , wherein the carrier has a specific surface area of 50 to 2000 m/g.4. The device according to claim 1 , wherein the organic compound is an alcohol or an organic hydride.5. The device according to claim 4 , wherein the alcohol is isopropanol.6. The device according to claim 4 , wherein the organic hydride is methylcyclohexane.7. The device according to claim 1 , which is for hydrogen generation.8. The device according to claim 1 , which is for aromatization.9. The device according to claim 1 , which is for hydrogenation.10. A catalyst for microwave irradiation claim 1 , the catalyst being a molded catalyst containing a noble metal supported on a carrier that has an average particle diameter larger than 100 μm.11. A method for producing hydrogen claim 1 , the method comprising irradiating a solution containing an organic compound claim 1 , the solution passing through a catalyst holding section that holds a solid catalyst claim 1 , with ...

SCR-Active Material Having Enhanced Thermal Stability

The invention relates to an SCR-active material, comprising a small-pore zeolite of the structure type levyne (LEV), aluminum oxide, and copper, characterized in that, based on the total material, the material contains 4 to 25 wt % of aluminum oxide. 1. An SCR-active material comprising(i) a small-pore zeolite of the levyne (LEV) structure type,(ii) aluminum oxide, and(iii) copper,wherein the copper is present in a first concentration on the aluminum oxide and in a second concentration on the small-pore zeolite,wherein it contains 4 to 25 wt % aluminum oxide, relative to the total SCR-active material.2. The SCR-active material according to claim 1 , wherein it contains 6 to 16 wt % aluminum oxide claim 1 , relative to the total SCR-active material.3. The SCR-active material according to claim 1 , wherein the total amount of copper claim 1 , calculated as CuO and relative to the total SCR-active material claim 1 , is 0.5 to 15 wt %.4. The SCR-active material according to claim 1 , wherein the small-pore zeolite of the levyne (LEV) structure type is an aluminosilicate.5. The SCR-active material according to claim 4 , wherein the small-pore zeolite of the levyne (LEV) structure type has an SAR value of 5 to 50.6. The SCR-active material according to claim 1 , wherein the small-pore zeolite of the levyne (LEV) structure type is a silicoaluminosilicate or an aluminophosphate.7. The SCR-active material according to claim 1 , wherein the atomic ratio of copper exchanged in the zeolite to skeleton aluminum in the zeolite is 0.25 to 0.6.8. The SCR-active material according to claim 1 , wherein the average crystallite size (d) of the small-pore zeolite of the levyne (LEV) structure type is 0.1 to 20 μm.9. The SCR-active material according to claim 1 , wherein the small-pore zeolite of the levyne (LEV) structure type forms a core claim 1 , and the aluminum oxide forms a shell surrounding this core.10. The SCR-active material according to claim 1 , wherein its specific surface ...

CATALYTICALLY DEGRADABLE PLASTIC AND USE OF SAME

A catalytically degradable plastic is described, with content of cellulose esters and also optionally of additives. A particular characterizing feature of this catalytically degradable plastic is that it contains a dispersed, catalytically active transition-metal-modified titanium dioxide. 115-. (canceled)16. A catalytically degradable plastics material comprising a catalytically active titanium dioxide modified by addition of at least one transition metal.17. The catalytically degradable plastics material as claimed in claim 16 , wherein the plastics material is a cellulose ester claim 16 , cellulose propionate claim 16 , cellulose butyrate claim 16 , cellulose acetate propionate claim 16 , cellulose acetate butyrate claim 16 , or mixtures thereof.18. The catalytically degradable plastics material as claimed in claim 17 , wherein the cellulose ester has an average degree of substitution (DS) of 1.5 to 3.0.19. The catalytically degradable plastics material as claimed in claim 17 , wherein the cellulose ester has an average degree of polymerization of 150 to 500.20. The catalytically degradable plastics material as claimed in claim 16 , further comprising a finely dispersed non-transition-metal-modified titanium dioxide.21. The catalytically degradable plastics material as claimed in claim 16 , wherein the transition-metal-modified titanium dioxide is transition-metal-doped on its surface.22. The catalytically degradable plastics material as claimed in claim 16 , wherein the transition-metal-modified titanium dioxide has a crystallite size of 5 to 150 nm.23. The catalytically degradable plastics material as claimed in claim 16 , wherein the transition-metal-modified titanium dioxide has a density of 3.0 to 5.0 g/cm claim 16 , as determined by ISO 787 claim 16 , part 10.24. The catalytically degradable plastics material as claimed in claim 16 , wherein the (BET) specific surface area of the transition-metal-modified titanium dioxide is greater than 100 m/g.25. The ...

CATALYST HAVING A HELICAL OUTER SHAPE, IMPROVING HYDRODYNAMICS IN REACTORS

A catalyst for catalytic reactors of which the outer shape is a helix with n blades, where n is greater than or equal to 1, wherein the stack void fraction percentage is between 75% and 85% and the surface area/volume ratio is greater than 1000 square meters/square meters. 19.-. (canceled)10. A catalyst for catalytic reactors , the outer shape of which is a helicoid having n blades with n≧_1 , wherein the void fraction percentage of the packing is between 75% and 85% , and wherein the surface area/volume ratio is greater than 1000 m/m , with said catalyst comprising a support and of an active phase deposited on the support.11. The catalyst of claim 10 , wherein the catalyst has a length between 5 mm and 40 mm and an equivalent cylinder diameter between 5 mm and 10 mm.12. The catalyst of claim 10 , wherein the surface area/volume ratio is greater than 2000 m/m.13. The catalyst of claim 10 , wherein the catalyst of helicoidal shape comprises between 1.5 and 10 turns.14. The catalyst of claim 10 , wherein the support is of inorganic oxide or mixture of inorganic oxides type.15. The catalyst of claim 14 , wherein the inorganic oxides are selected from the group consisting of AlO claim 14 , MgO claim 14 , CaO claim 14 , ZrO claim 14 , TiO claim 14 , CeOand CeO.16. The catalyst of claim 10 , wherein the active phase consists of metal particles selected from the group consisting of Ni claim 10 , Rh claim 10 , Pt claim 10 , Pd claim 10 , Co claim 10 , Mo claim 10 , Cu claim 10 , Fe claim 10 , and a mixture thereof.17. A catalytic reactor comprising a packing of catalysts as claimed in . This application is a 371 of International PCT Application PCT/FR2015/051394, filed May 27, 2015, which claims priority to French Patent Application No. 1454934, filed May 30, 2015, the entire contents of which are incorporated herein by reference.The present invention relates to novel catalyst structures.A catalyst is a material that converts reactants to product through repeated and ...

Catalyst and process for the production of diesel fuel from natural gas, natural gas liquids, or other gaseous feedstocks

A unique process and catalyst is described that operates efficiently for the direct production of a high cetane diesel type fuel or diesel type blending stock from stochiometric mixtures of hydrogen and carbon monoxide. This invention allows for, but is not limited to, the economical and efficient production high quality diesel type fuels from small or distributed fuel production plants that have an annual production capacity of less than 10,000 barrels of product per day, by eliminating traditional wax upgrading processes. This catalytic process is ideal for distributed diesel fuel production plants such as gas to liquids production and other applications that require optimized economics based on supporting distributed feedstock resources. 3. A process for the production of a hydrocarbon mixture comprising; a pore diameter greater than 80 angstroms and;', 'a crush strength of greater than 3 lbs/mm and;', 'a BET surface area of greater than 110 m2/g;', 'a dispersion value between 2% and 10%,, 'reacting a feed gas that contains hydrogen and carbon monoxide with a catalyst having,'}producing a product stream comprising light gases, diesel fuel and a wax from reacting the feed gas with the supported catalyst.4. The process of claim 1 , wherein the catalyst is reduced with hydrogen at temperatures below 650 F.5. The process of claim 1 , wherein the diesel fuel fraction produced is about ⅔ of the non-gas product produced.6. The process of claim 1 , wherein the supported catalyst comprises a lobed support with more than four lobes and an effective pellet radius of less than 600 microns.7. The process of claim 4 , where all of the lobes are not equal lengths.8. The process of claim 4 , wherein the supported catalyst further comprises about 0.01 weight percent to about 2.0 weight percent of a promoter selected from the group consisting of cerium claim 4 , ruthenium claim 4 , lanthanum claim 4 , platinum claim 4 , rhenium. gold claim 4 , nickel claim 4 , or rhodium and a ...

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

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

METHODS OF PRODUCING ORGANOSILICA MATERIALS AND USES THEREOF

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

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

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

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

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

HIGH GEOMETRIC SURFACE AREA CATALYSTS FOR VINYL ACETATE MONOMER PRODUCTION

A catalyst includes a support, where the support includes an external surface, about 60 wt % to about 99 wt % silica, and about 1.0 wt % to about 5.0 wt % alumina. A catalytic layer is disposed within the support adjacent to the external surface, where the catalytic layer further includes Pd, Au, and potassium acetate (KOAc). In the catalyst, (a) the KOAc is from about 60 kg/mto about 150 kg/mof the catalyst; or (b) the catalytic layer has an average thickness from about 50 μm to about 150 μm; or (c) both (a) and (b). The catalyst also possesses a Brunauer-Emmett-Teller surface area of about 130 m/g to about 300 m/g and a geometric surface area per packed bed volume from about 550 m/mto about 1500 m/m. The catalyst is highly active for the synthesis of vinyl acetate monomer and exhibits a high selectivity for vinyl acetate monomer. 1. A catalyst comprising: an external surface;', 'about 60 wt % to about 99 wt % silica; and', 'about 1.0 wt % to about 5.0 wt % alumina;, 'a support comprisinga catalytic layer disposed within the support adjacent to the external surface, where the catalytic layer further comprises Pd, Au, and potassium acetate (KOAc);{'sup': 2', '2, 'a Brunauer-Emmett-Teller surface area of about 130 m/g to about 300 m/g; and'}{'sup': 2', '3', '2', '3, 'a geometric surface area per packed bed volume from about 550 m/mto about 1500 m/m;'} [{'sup': 3', '3, '(a) the KOAc is from about 60 kg/mto about 150 kg/mof the catalyst; or'}, '(b) the catalytic layer has an average thickness from about 50 μm to about 150 μm, or', {'sup': 3', '3, '(c) the KOAc is from about 60 kg/mto about 150 kg/mof the catalyst and the catalytic layer has an average thickness from about 50 μm to about 150 μm.'}], 'wherein'}2. The catalyst of claim 1 , wherein the KOAc is from about 65 kg/mto about 100 kg/mof the catalyst.34-. (canceled)5. The catalyst of claim 1 , wherein the catalytic layer has an average thickness from about 100 μm to about 200 μm.6. The catalyst of claim 1 , ...

FILTRATION MEDIA FOR REMOVING CHLORAMINE, CHLORINE, AND AMMONIA, AND METHOD OF MAKING THE SAME

An activated carbon-based media for efficient removal of chloramines as well as chlorine and ammonia from an aqueous stream is presented, and a method for making the same. The method involves preparing activated carbon that remove chloramines efficiently from chloramine-rich aqueous media. In particular, this application relates to the use of high performance catalytically active carbon for an efficient removal of chloramine from drinking water in the form of a solid carbon block or granular carbon media. The activated carbon is treated with a nitrogen-rich compound, such as, melamine. 1. A method of making catalytically activated carbon particles comprising:providing a starting material in the form of an activated carbonaceous product;soaking said activated carbonaceous product in an acid solution to form acid treated carbon;drying said acid treated carbon;exposing said acid treated carbon to a nitrogen-rich compound to form nitrogen-rich impregnated carbon particles;heating said nitrogen-rich impregnated carbon particles in an inert atmosphere; andcooling said impregnated carbon particles to form catalytically activated nitrogen-rich carbon particles that remove chloramines, chlorine, and/or ammonia from aqueous media.2. The method of wherein said activated carbonaceous product includes coconut based activated carbon or coal based activated carbon in either granular (GAC) or powdered (PAC) form.3. The method of wherein said activated carbonaceous product has a surface area of ranging from about 800 m/g to about 1300 m/g.4. The method of wherein said step of soaking said activated carbonaceous product in an acid solution includes soaking in 15% nitric acid for approximately three hours.5. The method of wherein said step of drying said acid treated carbon includes drying until moisture content of said acid treated carbon is about or less than two (2) %.6. The method of wherein said step of drying said acid treated carbon includes drying at a temperature of ...

Catalyst and process for the production of diesel fuel from natural gas, natural gas liquids, or other gaseous feedstocks

A unique process and catalyst is described that operates efficiently for the direct production of a high cetane diesel type fuel or diesel type blending stock from stochiometric mixtures of hydrogen and carbon monoxide. This invention allows for, but is not limited to, the economical and efficient production high quality diesel type fuels from small or distributed fuel production plants that have an annual production capacity of less than 10,000 barrels of product per day, by eliminating traditional wax upgrading processes. This catalytic process is ideal for distributed diesel fuel production plants such as gas to liquids production and other applications that require optimized economics based on supporting distributed feedstock resources. 3. A process for the production of a hydrocarbon mixture comprising: a pore diameter greater than 80 angstroms and;', 'a crush strength of greater than 3 lbs/mm and;', 'a BET surface area of greater than 110 m2/g;', 'a dispersion value between 2% and 10%,, 'reacting a feed gas that contains hydrogen and carbon monoxide with a catalyst having,'}producing a product stream comprising light gases, diesel fuel and a wax from reacting the feed gas with the supported catalyst.4. The process of claim 1 , wherein the catalyst is reduced with hydrogen at temperatures below 650 F.5. The process of claim 1 , wherein the diesel fuel fraction produced is about ⅔ of the non-gas product produced.6. The process of claim 1 , wherein the supported catalyst comprises a lobed support with more than four lobes and an effective pellet radius of less than 600 microns.7. The process of claim 4 , where all of the lobes are not equal lengths.8. The process of claim 4 , wherein the supported catalyst further comprises about 0.01 weight percent to about 2.0 weight percent of a promoter selected from the group consisting of cerium claim 4 , ruthenium claim 4 , lanthanum claim 4 , platinum claim 4 , rhenium claim 4 , gold claim 4 , nickel claim 4 , or rhodium ...

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

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

CATALYTIC ACTIVATED CARBON STRUCTURES AND METHODS OF USE AND MANUFACTURE

The present disclosure relates generally to catalytic activated carbon structures and the methods of removing sulfur-containing compounds from fluid stream using such catalytic activated carbon structures. In certain aspects, the catalytic activated carbon structure comprise nitrogen-enriched activated carbon, cuprous oxide, and a binder, wherein the nitrogen-enriched activated carbon includes from about 0.5% to about 10% by weight of nitrogen based on total weight of the nitrogen-enriched activated carbon, at least about 30% by weight of the nitrogen are aromatic nitrogen species having a binding energy of at least 398.0 eV as determined by XPS. 1. A catalytic activated carbon material comprising:a matrix including nitrogen-enriched activated carbon, cuprous oxide, and a binder,wherein the nitrogen-enriched activated carbon includes from about 0.5% to about 10% by weight of nitrogen based on total weight of the nitrogen-enriched activated carbon, at least about 30% by weight of the nitrogen are aromatic nitrogen species having a binding energy of at least 398.0 eV as determined by XPS, andwherein the matrix material is formed into a three-dimensional structure.2. The material of claim 1 , wherein the material comprises the nitrogen-enriched activated carbon in an amount of from 10% to about 80% by weight based on total weight of the material.3. The material of claim 1 , wherein the material comprises the cuprous oxide in an amount of from 5% to about 50% by weight based on total weight of the material.4. The material of claim 1 , wherein the cuprous oxide has a D90 particle size of less than about 40 microns.5. The material of claim 1 , wherein the three-dimensional structure is a honeycomb having a cell density of from about 10 to about 1500 cells per square inch.6. The material of claim 5 , wherein the material has a B.E.T. surface area of from about 200 m/g to about 3000 m/g.7. The material of claim 1 , wherein at least about 50% by weight of the nitrogen are ...

Organosilica materials and uses thereof

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

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 ...

TRANSITION METAL(S) CATALYST SUPPORTED ON NITROGEN-DOPED MESOPOROUS CARBON AND ITS USE IN CATALYTIC TRANSFER HYDROGENATION REACTIONS

The present invention discloses a novel transition metal(s) catalyst supported on nitrogen-doped mesoporous carbon and a process for the preparation of the same. Further, the present invention discloses use of transition metal(s) supported on nitrogen-doped mesoporous carbon catalyst in catalytic transfer hydrogenation reaction. The invention also discloses an improved process for the synthesis of 2,5-Dimethylfuran (DMF) and 2-Methylfuran (MF) from 5-hydroxymethylfurfural (HMF) and furfural respectively, using alcohols as hydrogen donor over a transition metal supported on nitrogen-doped mesoporous carbon, especially ruthenium supported on nitrogen-doped mesoporous carbon without using any co-catalysts. 1. A catalyst composition comprising;a transition metal supported on nitrogen doped mesoporous carbon; wherein the transition metal(s) in the range of 0.5 to 10 weight % of the catalyst.2. The catalyst composition as claimed in claim 1 , wherein the transition metal is selected from the group consisting of Ru claim 1 , Pt claim 1 , Pd claim 1 , Rh claim 1 , Au claim 1 , Ag claim 1 , Os claim 1 , Ir claim 1 , Cu claim 1 , Ni claim 1 , Re claim 1 , Cr claim 1 , Mn claim 1 , Fe claim 1 , Zn claim 1 , Co; either alone or in combination of any two or more metals3. The catalyst composition as claimed in claim 1 , wherein BET surface area of the transition metal(s) catalyst in the range of 30-1200 m/g.4. The catalyst composition as claimed in claim 3 , wherein the BET surface area of the transition metal(s) catalyst in the range of 36 to 1200 m/g.5. The catalyst composition as claimed in claim 1 , wherein total pore volume of the transition metal(s) catalyst in the range of 0.07 to 1.2 cc/g.6. The catalyst composition as claimed in claim 1 , wherein average particle/crystal size of the transition metal(s) in the range of 1 to 10 nm7. A process for synthesis of metal(s)-nitrogen doped mesoporous carbon catalyst as claimed in comprising the steps of;a. dispersing nitrogen ...

CRYSTALLINE HIGH DEGREE OF CONDENSATION TITANIUM-BASED INORGANIC-ORGANIC HYBRID SOLID MOF MATERIAL, METHOD FOR PREPARING SAME AND USES THEREOF

The present invention relates to a water-stable Titanium-based metal-organic framework (MOF) material having a high degree of condensation, i.e. an oxo to Ti ratio (or oxo to metal ratio, in the case of doped Ti-based MOFs) >1.0; a process of preparing same and uses thereof, particularly for heterogeneously catalyzed chemical reactions, for gas storage/separation/purification, for information storage, laser printing or as an oxygen indicator, or as proton conductive material (fuel cells), optoelectronic material (photovoltaic cells including Grätzel cells), as a matrix for encapsulating active principles (medicaments, cosmetics), or else as sensing material. 1. A crystalline titanium-based inorganic-organic hybrid metal-organic framework (MOF) material constituted of a three-dimensional succession of building units of formula I:{'br': None, 'sub': a', 'b', 'x', 'y', '0, 'i': '.n', 'MOLASolv\u2003\u2003(I)'} each occurrence of M independently represents Ti or another metal; such as Cu, Co, Ni, Mn, V, Cr, Fe, Ru, Sn, or Nb; wherein at least 60% of M atoms in the MOF material are Ti atoms;', {'sub': '6', 'each occurrence of L independently represents a bis-Caryl-containing tetracarboxylate ligand;'}, {'sub': 2', '2', '2', '3', '3', '1-12', '1-12', '6-10', '5-10, 'sup': −', '−', '−', '2', '−', '2', '−', '2, 'each occurrence of A independently represents a ligand comprising HCO or MeCO; wherein a subset of A ligands in the MOF material may be replaced by ligands independently comprising OH, HO, R—(SO), R—(PO)H, wherein R, for each occurrence, independently represents OH, Calkyl, Cheteroalkyl, Caryl, Cheteroaryl; where each of the foregoing alkyl and heteroalkyl moiety may be linear or branched and cyclic or acyclic;'}, 'a represents the number of M atoms in the building unit;', 'b represents the number of O atoms in the building unit;', 'x represents the number of L ligands in the building unit;', 'y represents the number of A ligands in the building unit;', 'n ...

Carbon Supported Cobalt and Molybdenum Catalyst

The present invention relates to a catalyst composition comprising cobalt molybdenum and optionally one or more elements selected from the group consisting of alkali metals and alkaline earth metals on a carbon support wherein said cobalt and molybdenum are in their metallic form. It was surprisingly found that the selectivity for alcohols can be increased by using the carbon supported cobalt molybdenum catalyst as described herein in a process for producing alcohols from a feed stream comprising hydrogen and carbon monoxide. Furthermore, it was found that the catalyst of the present invention has a decreased selectivity for COand can be operated at relatively low temperature when compared to conventional catalysts. Moreover, a method for preparing the carbon supported cobalt molybdenum catalyst composition and a process for producing alcohols using said carbon supported cobalt molybdenum catalyst composition is provided. 113-. (canceled)14. A catalyst composition comprising formula CoMoMC , wherein M is one or more elements selected from the group consisting of alkali metal and alkaline earth metal and C is an activated carbon support , wherein the relative molar ratios of the elements in the formula are as follows:a is 1E-3-0.3;b is 1E-3-0.9;c is 0-1E-2; and{'sup': '2', 'wherein the Co and Mo are in their metallic form and wherein the catalyst composition has a BET surface area of at least 320 m/g.'}15. The catalyst composition according to claim 14 , wherein M is present and is selected from the group consisting of potassium (K) claim 14 , sodium (Na) claim 14 , calcium (Ca). and magnesium (Mg).16. The catalyst composition according to claim 14 , wherein:a is 1E-2-0.3; andb is 5E-3-0.9.17. The catalyst composition according to claim 14 , wherein the catalyst composition has a BET surface area of 350-1200 m/g.18. The catalyst composition according to claim 14 , wherein the Co and/or Mo are not in sulphide form.19. The catalyst composition according to claim 14 , ...

Structure

A structure includes a base material; a surface layer that contains a binder resin and a titanium compound particle having absorption at 450 nm and 750 nm in a visible absorption spectrum and a BET specific surface area within a range of 100 m 2 /g to 1200 m 2 /g.

Catalyst To Attain Low Sulfur Gasoline

This invention relates to a hydrodesulfurization catalyst, a method for preparing the catalyst, and a method for the preparation of low sulfur gasoline fuel with minimal loss of RON. The catalyst particles include a group VIB metal and a support material having relatively high surface area, and optionally includes one or more group VIIIB metal. The method for preparing the catalyst allows for greater loading of the active metal species on the surface of the support material under aqueous reaction conditions.

PENTASIL-TYPE ZEOLITE AND PRODUCTION METHOD THEREFOR

Provided are a pentasil-type zeolite that is less likely to adsorb water compared to conventional zeolites and has excellent strength when used as a molded body, and a method for producing the pentasil-type zeolite. 1. A pentasil-type zeolite having a water adsorption amount of 4.0 g/100 g-zeolite or less under the conditions of 25° C. and a relative humidity of 90% and having a major axis diameter of primary particles of from 0.2 μm to 4.0 μm.2. The pentasil-type zeolite according to claim 1 , wherein the pentasil-type zeolite has an aspect ratio of primary particles of from 1.0 to 3.0.3. The pentasil-type zeolite according to claim 1 , wherein the pentasil-type zeolite has a ratio SiO/AlO(molar ratio) of 200 or higher.4. The pentasil-type zeolite according to claim 1 , wherein the pentasil-type zeolite has a BET specific surface area of 300 m/g or larger.5. The pentasil-type zeolite according to claim 1 , wherein the pentasil-type zeolite has a content of NaO of 1.00 percent by weight or less.6. A method for producing the pentasil-type zeolite according to claim 1 , comprising:crystallizing a mixture including a silicon source, an amine as a structure-directing agent, and an alkali source, the mixture including no fluorine source;bringing a zeolite into contact with an alkali solution at pH 10 to 14; andcalcining the zeolite at a temperature of 500° C. to 1000° C. under a flow of water vapor.7. The method for producing the pentasil-type zeolite according to claim 6 , wherein the amine is n-propylamine claim 6 , dipropylamine claim 6 , or tripropylamine.8. The method for producing the pentasil-type zeolite according to claim 6 , wherein the crystallization temperature is 160° C. or lower. The present invention relates to a pentasil-type zeolite and a method for producing the same. More particularly, the invention relates to a pentasil-type zeolite which has a small water adsorption amount and is appropriate for use applications where high hydrophobicity is required ...

NITROGEN AND PHOSPHOROUS DOPED CARBON SUPPORTED NANOPARTICLE PLATINUM ELECTROCATALYST AND METHOD OF MAKING

A platinum-carbon electrocatalyst material comprising a carbon support having a minimum BET surface area of 1000 m/g, a nitrogen content of at least 2.5 weight percent, which is present in the form of pyridine, pyridone or pyrrole, a phosphorous content of at least 3 weight percent, which is present in the form of phosphate and phosphonate, and a plurality of platinum nanoparticles dispersed on the carbon support having a maximum average particle diameter of 1.5 nm. 1. A platinum-carbon electrocatalyst material comprising:{'sup': '2', '(a) a carbon support having a minimum BET surface area of 1000 m/g;'}(b) a nitrogen content of at least 2.5 weight percent, which is present in the form of pyridine, pyridone or pyrrole;(c) a phosphorous content of at least 3 weight percent, which is present in the form of phosphate and phosphonate; and(d) a plurality of platinum nanoparticles dispersed on the carbon support having a maximum average particle diameter of 1.5 nm.2. The platinum-carbon electrocatalyst material of further comprising: a DFT micropore volume from 0.3 to 0.45.3. The platinum-carbon electrocatalyst material of further comprising: pore widths from 1 to 100 nm.4. The platinum-carbon electrocatalyst material of further comprising: pore widths from 2 to 50 nm.5. The platinum-carbon electrocatalyst material of further comprising: pore widths in a range from 1 to 5 nm.6. The platinum-carbon electrocatalyst material of further comprising: a minimum BET surface area of 1400 m/g.7. A method of making a platinum-carbon electrocatalyst material comprising a carbon support having a minimum BET surface area of 1000 m/g; a nitrogen content of at least 2.5 weight percent claim 1 , which is present in the form of pyridine claim 1 , pyridone or pyrrole; a phosphorous content of at least 3 weight percent claim 1 , which is present in the form of phosphate and phosphonate; and a plurality of platinum nanoparticles dispersed on the carbon support having a maximum average ...

HIERARCHICAL POROUS MONOLITHS AND METHODS FOR THEIR PREPARATION AND USE

Methods of forming a hierarchical porous monolith are provided. The methods include mixing a monomer, a silica precursor and a catalyst in a solvent to form a mixture. The methods also include adding a gelling agent to the mixture to form a polymer-silica composite gel. The polymer-silica composite gel undergoes a phase separation to separate from the solvent and the unreacted silica precursor. The method further includes drying the polymer-silica composite gel to evaporate the solvent to form a polymer-silica monolith and processing the polymer-silica monolith to form at least one of a polymer monolith, a carbon monolith, a silica monolith and a carbon-silica monolith. 1. A method of forming a hierarchical porous monolith , the method comprising:mixing a monomer, a silica precursor and a catalyst in a solvent to form a mixture;adding a gelling agent to the mixture to form a polymer-silica composite gel, wherein the polymer-silica composite gel undergoes a phase separation to separate from the solvent and the unreacted silica precursor;drying the polymer-silica composite gel to evaporate the solvent to form a polymer-silica monolith; andprocessing the polymer-silica monolith to form at least one of a polymer monolith, a carbon monolith, a silica monolith and a carbon-silica monolith.2. The method of claim 1 , wherein mixing the monomer comprises mixing resorcinol (CHO) claim 1 , phloroglucinol (CHO) claim 1 , acrylonitrile (CHN) claim 1 , vinyl alcohol (CHO) claim 1 , methyl methacrylate (CHO) claim 1 , or combinations of any two or more thereof.3. The method of claim 1 , wherein adding the gelling agent comprises adding formaldehyde (CHO) claim 1 , dimethyl sulfoxide (CHOS) claim 1 , water (HO) claim 1 , dimethylformamide ((CH)NC(O)H) claim 1 , or combinations of any two or more thereof.4. The method of claim 1 , wherein mixing the silica precursor comprises mixing tetraethyl orthosilicate (TEOS) claim 1 , tetramethyl orthosilicate (TMOS) claim 1 , or combinations ...

Trans-metallated mof catalyst

A metal organic framework comprising zinc (II) ions and second metal ions, such as iron (II) ions, cobalt (II) ions, and copper (II) ions as nodes or clusters and coordinated 1,3,5-benzenetricarboxylic acid struts or linkers between them forming a porous coordination network in the form of polyhedral crystals that are isostructural to HKUST-1. Transmetallation processes for producing the metal organic frameworks, as well as methods for applications of the metal organic frameworks as catalysts, specifically catalysts for the oxidation of cyclic hydrocarbons, such as toluene, cyclohexane, and methylcyclohexane.

Porous Carbon Material, Method for Producing Same, and Synthesis Reaction Catalyst

A porous carbon material, 1. A porous carbon material ,wherein a half width (2θ) of a diffraction peak (10×) (38° to 49°) by X-ray diffraction is 4.2° or less, and{'sup': 3', '3, 'wherein a ratio (mesopore volume/micropore volume) of a mesopore volume (cm/g) measured by a BJH method to a micropore volume (cm/g) measured by a HK method is 1.20 or more.'}2. The porous carbon material according to claim 1 , wherein the porous carbon material is derived from a plant.3. The porous carbon material according to claim 1 , wherein the porous carbon material is derived from chaff.4. The porous carbon material according to claim 1 , wherein the porous carbon material is a carrier for a catalyst.5. A method for producing the porous carbon material according to claim 1 , the method comprising:removing, from a raw material containing a silicon component, the silicon component by an acid treatment or an alkali treatment, and then performing a carbonization treatment.6. The method for producing the porous carbon material according to claim 5 , wherein an activation treatment is performed after the carbonization treatment.7. A method for producing the porous carbon material according to claim 1 , the method comprising:performing a carbonization treatment on a raw material containing a silicon component, then removing the silicon component from an obtained carbonized product by an acid treatment or an alkali treatment, and then performing an activation treatment.8. The method for producing the porous carbon material according to claim 6 , wherein a heat treatment is performed after the activation treatment.9. The method for producing the porous carbon material according to claim 8 , wherein a temperature of the heat treatment is 1 claim 8 ,200° C. or higher.10. The method for producing the porous carbon material according to claim 5 , wherein a temperature of the carbonization treatment is 600° C. or higher.11. A synthesis reaction catalyst comprising:{'claim-ref': {'@idref': 'CLM- ...

CATALYST SYSTEM BASED ON SPHERICAL ACTIVATED CARBON AS A CARRIER AND USE THEREOF

The invention relates to a method for producing a catalyst system having at least one catalytically active component, wherein the catalytically active component comprises at least one metal, wherein first a spherical activated carbon used as a catalyst carrier is subjected to an oxidation. Subsequently, the catalytically active component is applied, optionally followed by a reduction of the catalyst system obtained in said manner. 114-. (canceled)15. A method of preparing a catalyst system comprising at least one catalytically active component , wherein at least one catalytically active component is fixed on a catalyst carrier , wherein the catalytically active component comprises at least one metal ,wherein said method comprises the following steps in the hereinbelow defined sequence (a) to (d):{'sup': 3', '3', '2', '2, '(a) providing a spherical activated carbon as a catalyst carrier, wherein the spherical activated carbon is a polymer-based spherical activated carbon, wherein the activated carbon has a Gurvich total pore volume in the range from 0.5 cm/g to 4 cm/g, wherein 10% to 85% of the Gurvich total pore volume of the activated carbon is formed by pores having pore diameters in the range from 2 nm to 50 nm, and wherein the activated carbon has a specific BET surface area in the range from 800 m/g to 3500 m/g and a particle size in the range from 0.05 mm to 2 mm; then'}(b) surface-oxidizing the spherical activated carbon provided in step (a), wherein the surface oxidation of the activated carbon leads to a formation of oxygen-containing functional groups on the surface of the activated carbon, wherein the surface oxidation of the activated carbon is performed via at least one oxidizing agent, wherein the oxidizing agent is selected from the group of hydrogen peroxide, nitric acid and sulfuric acid and their combinations and wherein the oxidizing agent is applied in liquid form in the form of solutions or dispersions, and wherein the surface oxidation is ...

PROCESS FOR THE SYNTHESIS OF TRIFLUOROETHYLENE

A catalytic process for the synthesis of trifluoroethylene from chlorotrifluoroethylene which comprises contacting chlorotrifluoroethylene with hydrogen in the presence of a catalyst consisting of palladium or platinum supported on extruded activated carbon. 14-. (canceled)5. A catalyst consisting of palladium or platinum , supported on activated carbon , wherein the activated carbon is extruded activated carbon.6. The catalyst according to claim 5 , wherein the amount of said palladium or said platinum supported on the extruded activated carbon is between 0.05 and 5% by weight.7. The catalyst according to claim 6 , wherein the amount of said palladium or said platinum supported on the extruded activated carbon is between 0.1 and 4% by weight.8. The catalyst according to claim 7 , wherein the amount of said palladium or said platinum supported on the extruded activated carbon is between 0.2 and 3% by weight9. The catalyst according to claim 8 , wherein the amount of said palladium or said platinum supported on the extruded activated carbon is between 0.3 and 2.5% by weight.10. The catalyst according to claim 5 , wherein the extruded activated carbon has a surface area of between 500 and 1500 m/g.11. The catalyst according to claim 5 , wherein the extruded activated carbon is in the form of pellets having a pellet diameter between 0.8 and 130 mm.12. The catalyst according to claim 5 , consisting of the palladium supported on the extruded activated carbon.13. The catalyst according to claim 6 , consisting of the palladium supported on the extruded activated carbon.14. The catalyst according to claim 7 , consisting of the palladium supported on the extruded activated carbon.15. The catalyst according to claim 8 , consisting of the palladium supported on the extruded activated carbon.16. The catalyst according to claim 9 , consisting of the palladium supported on the extruded activated carbon. This application claims priority to European application No. 10168130.2 filed ...

COMPOSITIONS FOR REMOVING HYDROCARBONS AND HALOGENATED HYDROCARBONS FROM CONTAMINATED ENVIRONMENTS

A composition for in situ remediation of soil and groundwater contaminated with hydrocarbons. The composition includes an adsorbent, such as activated carbon, capable of adsorbing the hydrocarbons. The composition also includes a sulfate-containing compound that releases sulfate over a period of time, e.g., a time-release compound that may include calcium sulfate. The composition includes a nutrient system for promoting growth of facultative anaerobes, in the soil or provided in the composition itself. In some embodiments, the nutrient system includes a sulfide scavenging agent such as iron sulfate. In the same or other embodiments, the nutrient system includes at least one of a nitrogen source and a phosphorous source. 1. A composition for in situ bioremediation of soil contaminated with hydrocarbons , comprising:an adsorbent capable of adsorbing the hydrocarbons during the in situ bioremediation of the soil;a non-toxic compound that releases, into the soil, sulfate over a period of time; anda nutrient system for promoting growth of facultative anaerobes, when the composition is placed in the soil as part of the in situ bioremediation, capable of metabolizing the hydrocarbons.2. The composition of claim 1 , wherein the adsorbent comprises activated carbon.3. The composition of claim 1 , wherein the sulfate-containing compound comprises calcium sulfate.4. The composition of claim 1 , wherein the nutrient system includes a sulfide scavenging agent.5. The composition of claim 4 , wherein the sulfide scavenging agent comprises iron sulfate.6. The composition of claim 1 , wherein the nutrient system includes a nitrogen source.7. The composition of claim 6 , wherein the nitrogen source comprises an ammonium salt.8. The composition of claim 1 , wherein the nutrient system includes a phosphorous source and wherein and the phosphorous source comprises at least one of a monobasic alkali-metal phosphate and ammonium phosphate.9. The composition of claim 1 , wherein the ...

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 ...

AROMATIC HYDROGENATION CATALYSTS AND USES THEREOF

Hydrogenation catalysts for aromatic hydrogenation including an organosilica material support, which is a polymer comprising independent units of a monomer of Formula [ZOZOSiCH](I), wherein each Zand Zindependently represent a hydrogen atom, a C-Calkyl group or a bond to a silicon atom of another monomer; and at least one catalyst metal are provided herein. Methods of making the hydrogenation catalysts and processes of using, e.g., aromatic hydrogenation, the hydrogenation catalyst are also provided herein. 125.-. (canceled)26. A method of making a hydrogenation catalyst for aromatic hydrogenation , the method comprising:a) providing an aqueous mixture that contains essentially no structure directing agent and/or porogen,{'sup': 15', '16', '15', '16, 'sub': 2', '3', '1', '4', '1', '4', '1', '4, '(b) adding at least one compound of Formula [ZZSiCH](VII) into the aqueous mixture to form a solution, wherein each Zrepresents a C-Calkoxy group and each Zrepresents a C-Calkoxy group or a C-Calkyl group;'}(c) aging the solution to produce a pre-product;{'sup': 1', '2', '1', '2, 'sub': 2', '3', '1', '4, '(d) drying the pre-product to obtain an organosilica material support which is a polymer comprising independent units of a monomer of Formula [ZOZOSiCH](I), wherein each Zand Zindependently represent a hydrogen atom, a C-Calkyl group or a bond to a silicon atom of another monomer, wherein the organosilica material support has an X-ray diffraction pattern with one peak between 1 and 3 degrees 2θ and no peaks in the range of from 3 to 20 degrees 2θ; and'}(e) impregnating the organosilica material support with at least one catalyst metal selected from the group consisting of a Group 8 metal, a Group 9 metal, a Group 10 metal and a combination thereof.27. The method of claim 26 , wherein each Zrepresents a C-Calkoxy group.28. The method of claim 27 , wherein each Zrepresents a C-Calkoxy group.29. The method of claim 28 , wherein each Zrepresents a C-Calkoxy group.30. The method ...

Methane Oxidation Catalyst and Method of Using Same

Provided herein is a methane oxidation catalyst having a support comprising alumina doped with lanthanum and comprising platinum and palladium as active phases. The platinum and palladium are present in the catalyst at an amount effective for producing an exhaust stream from a natural gas vehicle having reduced levels of methane. The catalyst disclosed herein may exhibit improvements in sulfur and water resistance. 1. A method for reducing unburned methane in a gas stream resulting from methane combustion in a natural gas vehicle (NGV) , said gas stream comprising sulfur , said method comprising passing the gas stream through a methane oxidation catalyst having a support comprising alumina doped with lanthanum and comprising platinum and palladium as active phases , thereby producing an exhaust stream from said natural gas vehicle having reduced levels of methane relative to the gas stream resulting from methane combustion ,wherein the platinum and palladium are present in the methane oxidation catalyst at a weight ratio of Pt:Pd that is greater than 0.75:1.0.2. The method of claim 1 , wherein the gas stream resulting from the methane combustion has a temperature of between 350° C. and 600° C.3. The method of claim 1 , wherein the gas stream resulting from methane combustion comprises between 10 and 20 claim 1 ,000 ppm of methane.4. The method of claim 1 , wherein the gas stream resulting from methane combustion comprises oxygen.5. The method of claim 1 , wherein the gas stream resulting from methane combustion comprises water.6. The method of claim 1 , wherein the platinum is present in the methane oxidation catalyst at between 0.5 and 10 wt %.7. The method of claim 1 , wherein the palladium is present in the methane oxidation catalyst at between 0.5 and 10 wt %.8. The method of claim 1 , wherein the platinum and palladium are present in the methane oxidation catalyst at a concentration effective to reduce the methane content in the gas stream resulting from ...

METAL ORGANIC FRAMEWORKS AS CATALYSTS AND HYDROCARBON OXIDATION METHODS THEREOF

A metal organic framework comprising zinc (II) ions and second metal ions, such as iron (II) ions, cobalt (II) ions, and copper (II) ions as nodes or clusters and coordinated 1,3,5-benzenetricarboxylic acid struts or linkers between them forming a porous coordination network in the form of polyhedral crystals that are isostructural to HKUST-1. Transmetallation processes for producing the metal organic frameworks, as well as methods for applications of the metal organic frameworks as catalysts, specifically catalysts for the oxidation of cyclic hydrocarbons, such as toluene, cyclohexane, and methylcyclohexane. 1: A metal organic framework catalyst , comprising:zinc (II) ions;second metal ions which are not zinc (II) ions; andbenzene-1,3,5-tricarboxylic acid ligands;wherein the benzene-1,3,5-tricarboxylic acid ligands comprise carboxylate groups, each carboxylate group forming a coordinative bond to the zinc (II) ions or the second metal ions to form a coordination network in the form of porous polyhedral crystals that are isostructural to an HKUST-1 metal organic framework.2: The metal organic framework catalyst of claim 1 , wherein the second metal ions are at least one selected from the group consisting of iron (II) ions claim 1 , cobalt (II) ions claim 1 , and copper (II) ions.3: The metal organic framework catalyst of claim 1 , wherein the ratio of zinc (II) ions to the additional metal ions is in the range of 0.01 to 5.0.4: The metal organic framework catalyst of claim 1 , wherein the porous polyhedral crystals have pores with an average diameter of 0.2-2.0 nm and a BET surface area in the range of 500-3000 m/g.5: The metal organic framework catalyst of claim 1 , wherein the porous polyhedral crystals are octahedral or cubic with an average longest linear dimension in the range of 2-20 μm.6: The metal organic framework catalyst of claim 1 , which has a larger unit cell dimension a than the HKUST-1 metal organic framework.7: The metal organic framework catalyst ...

LOW-TEMPERATURE OXIDATION CATALYST

A catalyst for oxidizing a substance such as ethylene, carbon monoxide, or formaldehyde at high efficiency even at a low temperature of 100° C. or below, such as room temperature or below. Further, an oxidation catalyst of a low-temperature substance in which a noble metal and a metal halogen salt other than that of a noble metal are supported on a metal oxide carrier. 1. A low temperature oxidation catalyst comprisinga metal oxide carrier, anda noble metal and a halide of a metal other than noble metals, wherein said noble metal and said halide is supported on the carrier.2. The low temperature oxidation catalyst according to claim 1 , wherein the halogen comprises chlorine.3. The low temperature oxidation catalyst according to claim 1 , wherein the loading amount of the halide of the metal other than noble metals is 0.01% by weight or more based on the content of a halogen element in the halide claim 1 , relative to the total weight of the carrier and the noble metal.4. The low temperature oxidation catalyst according to claim 3 , wherein the loading amount of the halide of the metal other than noble metals is 0.02% by weight or more based on the content of the halogen element in the halide claim 3 , relative to the total weight of the carrier and the noble metal.5. The low temperature oxidation catalyst according to claim 1 , wherein the halide of the metal other than noble metals is a compound selected from the group consisting of alkali metal halides claim 1 , alkaline earth metal halides claim 1 , transition metal halides and halides of Group XIII elements except boron.6. The low temperature oxidation catalyst according to claim 1 , wherein the metal in the halide of the metal other than noble metals is one or more elements selected from the group consisting of calcium claim 1 , magnesium claim 1 , iron and aluminum.7. The low temperature oxidation catalyst according to claim 1 , wherein the noble metal is at least one element selected from the group ...

Catalyst to Attain Low Sulfur Gasoline

This invention relates to a hydrodesulfurization catalyst, a method for preparing the catalyst, and a method for the preparation of low sulfur gasoline fuel with minimal loss of RON. The catalyst particles include a group VIB metal and a support material having relatively high surface area, and optionally includes one or more group VIIIB metal. The method for preparing the catalyst allows for greater loading of the active metal species on the surface of the support material under aqueous reaction conditions. 1. A method for hydrodesulfurizing a petroleum based hydrocarbon distillate comprising:contacting the petroleum hydrocarbon distillate with hydrogen gas in the presence of a hydrodesulfurization catalyst;wherein the hydrodesulfurization catalyst comprises an activated carbon catalyst support material, a first metal selected from the group consisting of chromium, molybdenum and tungsten, and a second metal selected from the group consisting of iron, ruthenium, osmium, cobalt, rhenium, iridium, nickel, palladium and platinum;wherein the hydrodesulfurization catalyst comprises between about 10 and 30% by weight of the oxide form of the first metal and between about 1 and 10% by weight of the oxide form of the second metal.2. The method of wherein the hydrodesulfurization catalyst is prepared by the process comprising:preparing a mixture comprising at least one metal salt, a catalyst support and water, wherein the mixture is under vacuum;removing the water from the mixture and collecting the catalyst particles;calcinating the particles by heating the particles to a temperature of greater than about 200° C.; andpartially sulfiding the catalyst particles by contacting the calcined catalyst particles with a gas stream comprising up to about 5% by volume hydrogen sulfide;wherein the metal salt comprises a first metal selected from the group consisting of chromium, molybdenum, and tungsten.3. The method of wherein the hydrodesulfurization catalyst comprises at least ...

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

A wash coat is formed by combining platinum group metals (PGM) and an adhesive with a mixture of catalyst support materials according to the relationship (α)RE-Ce—ZrO 2 +(β)CZMLA+( 1 −α−β)RE-Al 2 O 3 . The RE-Ce—ZrO 2 is a commercial material of rare earth elements stabilized ceria zirconia having a weight ratio (α) ranging from 0 to about 0.7; CZMLA is a catalyst support material comprising a core support powder coated with a solid solution and has a weight ratio (β) ranging from about 0.2 to about 1 such that (α+β)≦1. RE-Al 2 O 3 is rare earth element stabilized alumina having a weight ratio equal to (1−α−β). The wash coat exhibits a lower activation temperature compared with traditional wash coat formulations by at least 50° C. This wash coat also requires less RE-Ce—ZrO 2 oxide and/or less PGM in the formulation for use as an emission control catalyst for gasoline and diesel engines.

CARBON MATERIAL FOR CATALYST SUPPORT USE

A carbon material for catalyst support use which, when used as a catalyst support, maintains a high porosity while being stable chemically, having electrical conductivity, being excellent in durability, and being excellent in diffusibility of the reaction starting materials and reaction products is provided. It is characterized by comprising dendritic carbon mesoporous structures which have 3D structures of branched carbon-containing rod shapes or carbon-containing ring shapes, having a pore size of 1 to 20 nm and a cumulative pore volume of 0.2 to 1.5 cc/g found by analyzing a nitrogen adsorption isotherm by the Dollimore-Heal method, and having a powder X-ray diffraction spectrum which has a peak corresponding to a 002 diffraction line of graphite between diffraction angles (2θ: degrees) of 20 to 30 degrees and has a peak with a half value width of 0.1 degree to 1.0 degree at 25.5 to 26.5 degrees. 1. A carbon material for catalyst support use comprising dendritic carbon mesoporous structures which have 3D structures of branched carbon-containing rod shapes or carbon-containing ring shapes ,having a pore size of 1 to 20 nm and a cumulative pore volume of 0.2 to 1.5 cc/g found by analyzing a nitrogen adsorption isotherm by the Dollimore-Heal method, andhaving a powder X-ray diffraction spectrum which has a peak corresponding to a 002 diffraction line of graphite between diffraction angles (2θ: degrees) of 20 to 30 degrees and has a peak with a half value width of 0.1 degree to 1.0 degree at 25.5 to 26.5 degrees.2. The carbon material for catalyst support use according to wherein{'sup': 2', '2, 'a BET specific surface area is 200 m/g to 1300 m/g and'}{'sub': 10', '10, 'sup': 2', '2', '31', '3', '−', '3, 'a ratio V/S (ml/m) of an amount of steam adsorption (ml/g) at 25° C. and a relative pressure of 10% (V) and a nitrogen adsorption BET specific surface area (m/g) of the carbon material (S) is 0.05×10to 1.0 ×10.'}3. A method for producing a carbon material for ...

ELECTRODE CATALYST, AND MEMBRANE ELECTRODE ASSEMBLY AND FUEL CELL USING ELECTRODE CATALYST

Provided is a catalyst that can exhibit high activity. The catalyst is an electrode catalyst having catalytic metals supported on a catalyst support, in which the catalytic metals include platinum and a metal component other than platinum; the electrode catalyst has mesopores having a mode radius of pore distribution of mesopores having a radius of 1 nm or more, of 1 nm or more and less than 2.5 nm; alloy microparticles of platinum and the metal component other than platinum are supported inside the mesopores; and a molar content ratio of platinum with respect to the metal component other than platinum in the alloy microparticles supported inside the mesopores is 1.0 to 10.0. 1. An electrode catalyst in which catalytic metals are supported on a catalyst support ,wherein the catalytic metals include platinum and a metal component other than platinum,the electrode catalyst has mesopores having a radius of 1 nm or more, with a mode radius of pore distribution of the mesopores being 1 nm or more and less than 2.5 nm,alloy microparticles of platinum and the metal component other than platinum are supported inside the mesopores, anda molar content ratio of platinum with respect to the metal component other than platinum in the alloy microparticles supported inside the mesopores is 1.0 to 10.0.2. The electrode catalyst according to claim 1 , wherein the electrode catalyst has a pore volume of the mesopores of 0.4 cc/g of the support or more.3. The electrode catalyst according to claim 1 , wherein the alloy microparticles supported inside the mesopores have an average diameter of 2.0 nm or more.4. The electrode catalyst according to claim 1 , wherein the alloy microparticles in the electrode catalyst have claim 1 , as an internal structure claim 1 , an intermetallic compound structure having platinum atoms and metal atoms other than platinum arranged with regularity.5. The electrode catalyst according to claim 4 , wherein the alloy microparticles in the electrode catalyst ...

PROCESSING OF HEAVY HYDROCARBON FEEDS

Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude. 115.-. (canceled)16. A process for producing a hydroprocessed product , comprising:{'sup': '−1', 'exposing a combined feedstock comprising a heavy oil feed component and at least about 5 wt % of a High Solvency Dispersive Power (HSDP) crude component to a hydroprocessing catalyst under effective fixed bed hydroprocessing conditions to form a hydroprocessed effluent, the effective fixed bed hydroprocessing conditions including a pressure of about 1500 psig (˜10.3 MPa) or less, a temperature of at least about 360° C., and a liquid hourly space velocity of the fraction of the combined feedstock boiling above 1050° F. (˜566° C.) of at least about 0.10 hr,'}the HSDP crude component having a TAN of at least about 0.3 and a solubility blending number of at least about 75, the HSDP crude component optionally comprising an aromatics content of at least about 50 wt %.17. The process of claim 16 , wherein the HSDP crude component has a 10% distillation point of at least about 800° F. (˜427° C.).18. The process of claim 16 , wherein the heavy oil feed component has a 10% distillation point of at least about 900° F. (˜482° C.).19. The process of claim 16 , wherein the effective fixed bed hydroprocessing conditions are ...

HYBRID REACTOR HEAVY PRODUCT UPGRADING METHOD WITH DISPERSED CATALYST UPTAKE

The invention concerns a process for the hydrotreatment of a heavy oil feed in at least one reactor containing a fixed bed catalyst, in which a solution containing a dispersed catalyst or a precursor of a dispersed catalyst is continuously introduced into said reactor, the particle size of said dispersed catalyst being in the range 1 nm to 100 μm. 1. A process for the hydrotreatment of a heavy oil feed in at least one reactor containing a fixed bed catalyst composed of an active phase deposited on a solid support , in which a solution containing a dispersed catalyst or a precursor of a dispersed catalyst is continuously introduced into said reactor , the particle size of said dispersed catalyst being in the range 1 nm to 100 μm , said fixed bed catalyst capturing said dispersed catalyst on its solid support.2. The process as claimed in claim 1 , in which the particle size of said dispersed catalyst is in the range 10 nm to 75 μm.3. The process as claimed in claim 1 , in which the feed is selected from feeds constituted by hydrocarbon fractions obtained from a crude oil or from atmospheric distillation of a crude oil or from vacuum distillation of a crude oil claim 1 , said feeds containing a fraction of at least 80% by weight of molecules having a boiling point of at least 300° C.4. The process as claimed in claim 1 , in which the hydrotreatment process is carried out at an absolute pressure in the range 2 MPa to 38 MPa and at a temperature in the range 300° C. to 550° C. claim 1 , and with an hourly space velocity (HSV) of the volume of feed with respect to the volume of catalyst in the range 0.05 hto 10 h.5. The process as claimed in claim 1 , in which said fixed bed catalyst contains one or more elements from groups 4 to 12 of the periodic table of the elements which are deposited on said solid support.6. The process as claimed in claim 5 , in which said solid support for the fixed bed catalyst is selected from amorphous solids selected from silica claim 5 , ...

PROCESSING OF HEAVY HYDROCARBON FEEDS

Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude. 120.-. (canceled)21. A process for producing a hydroprocessed product , comprising:passing a feedstock comprising resid to a first reactor operating at about 1000 psig (˜6.9 MPag) or less,demetallizing at least about 60 wt % and up of the feedstock to create a liquid product,passing the liquid product from the first reactor to a fractionator,separating out in the fractionator a heavy residuum fraction having a boiling point of about 1050° F. (˜566° C.),passing the heavy residuum fraction from the fractionator to a second reactor operating at from about 1500 psig (˜10.4 MPag) to about 3400 psig (˜23.5 MPag).22. The process of claim 21 , wherein the temperature of first reactor is between 650° F. (˜343° C.) and 850° F. (˜454° C.).23. The process of claim 21 , wherein demetallizing further comprises exposing the feedstock to a demetallization catalyst at a pressure of about 300 psig (˜2.1 MPag) to about 800 psig (˜5.6 MPag) and a temperature of about 600° F. (˜316° C.) to about 1000° F. (˜538° C.).24. The process of claim 23 , whereina) the demetallization catalyst has a mean pore diameter of 60 Å or less,{'sup': 2', '3, 'b) the demetallization catalyst comprises a catalyst with a surface area of at least ...

PALLADIUM CATALYST FOR OXIDATION OF METHANE AND METHOD OF PREPARATION AND USE THEREOF

This invention relates to a novel palladium catalyst for the substantially complete oxidative removal of methane from exhaust streams at low operating temperatures compared to other current palladium catalysts and to methods of preparing the catalyst. Use of the catalyst to remove methane from vehicle exhaust streams, crude oil production and processing exhaust streams, petroleum refining exhaust streams and natural gas production and processing exhaust streams. 1. A catalyst for methane oxidation , comprising:nanoparticulate palladium species;non-hierarchical ceria; and light-off at approximately 200° C.;', 'stability up to at least 800° C.', 'consistent catalytic activity to at least 800° C.; and', 'consistent catalytic activity for exhaust streams containing up to 15 wt % water to at least 800° C., 'wherein the catalyst is characterized by, 'non-hierarchical alumina;'}2. The catalyst according to claim 1 , wherein the catalyst comprises 0.5 to 5 wt % nanoparticulate palladium species and 0.5 to 5 wt % ceria claim 1 , both based on the quantity of alumina present.3. The catalyst according to claim 1 , wherein the catalyst comprises 5 wt % nanoparticulate palladium species and 5 wt % ceria claim 1 , both based on the quantity of alumina present.4. The catalyst of claim 1 , wherein the catalyst has a BET surface area of at least 88 m/g.5. A method of synthesizing the catalyst of claim 1 , comprising solution combustion synthesis.6. The catalyst of claim 5 , wherein the solution combustion synthesis comprises:Preparing a solution of a water-soluble palladium salt, a water soluble cerium salt, a water soluble aluminum salt and a reductant in distilled water;Applying external heat to the solution until self-sustained combustion is initiated;Removing the external heat source and permitting the self-sustained combustion to proceed to completion to provide a powder product; andCalcining the powder product in air at 800° C. for three hours.7. The method of claim 6 , ...

PRODUCTION OF BIOFUELS WITH NOVEL SALTS IMPREGNATED TIRE-DERIVED CARBON CATALYSTS

The invention provides a catalyst and a method for making the catalyst. The catalyst comprises a porous carbon composite impregnated with a salt. The catalyst comprises a porous carbon composite impregnated with a salt. 1. A catalyst comprising a porous carbon composite impregnated with a salt.2. The catalyst according to claim 1 , wherein the carbon composite contains a mixed meso-microporosity.3. The catalyst according to claim 1 , wherein the carbon composite has a specific surface area of between 1-2000 m/g.4. The catalyst according to claim 1 , wherein the carbon composite has a pore volume of 0.0100-0.1000 mg.5. The catalyst according to claim 1 , wherein the carbon composite is impregnated with a salt.6. The catalyst according to claim 5 , wherein the salt is a transition metal salt.7. The catalyst according to claim 6 , wherein the transition metal salt is ferric sulfate.8. The catalyst according to claim 1 , wherein the carbon composite is derived from waste tires.9. The catalyst according to claim 1 , wherein the group component of the salt is present on the surface of the porous carbon composite.10. A method for making a catalyst claim 1 , the method comprising:a. providing rubber pieces,b. optionally contacting the rubber pieces with a sulfonation bath to produce sulfonated rubber,c. pyrolyzing the rubber pieces or sulfonated rubber to produce a rubber-derived porous carbon composite, andd. impregnating the porous carbon composite with a salt to produce a catalyst comprising a porous carbon composite impregnated with a salt.11. The method according to claim 10 , wherein the rubber pieces are from waste tires.12. The method according to claim 10 , wherein the sulfonation bath comprises sulfuric acid.13. The method according to claim 10 , wherein the pyrolyzing temperature is from about at least 200° C. to 2400° C.14. The method according to claim 13 , wherein the salt is a transition metal salt.15. The method according to claim 14 , wherein the transition ...

Carbon Foam-Based Catalyst Support

A catalysis substrate, which includes an open cell carbon foam substrate having a geometric surface area of at least about 5000 m/m, wherein the substrate includes a catalytic metal. 1. A catalysis substrate which comprises an open cell carbon foam having a geometric surface area of at least about 5000 m/m , wherein the substrate comprises catalyst particles.2. The substrate of claim 1 , which is formed from foam starting materials selected from the group consisting of phenolic foam claim 1 , polyurethane foam claim 1 , polyacrylonitrile claim 1 , other acrylonitrile materials claim 1 , foams derived from organic gels.3. The substrate of claim 1 , wherein the catalyst particles comprise precious metals claim 1 , non-noble metal nano-scale catalytic particles claim 1 , or combinations thereof.4. The substrate of claim 3 , wherein the non-noble metal nano-scale catalytic particles comprise iron claim 3 , nickel claim 3 , manganese claim 3 , and combinations thereof claim 3 , and further wherein the non-noble metal nano-scale catalytic particles have an average diameter of no greater than about 20 nm.5. The substrate of claim 4 , wherein the non-noble metal nano-scale catalytic particles are present in chain agglomerations which have an aspect ratio of at least 700:1.6. The substrate of claim 1 , wherein the substrate has a permeability of at least about 12.0 darcys.7. The substrate of claim 3 , wherein the catalyst particles are incorporated into one or both of oxidative and reductive washcoats which are coated on the substrate.8. The substrate of claim 3 , wherein the catalyst particles are incorporated into the carbon foam which forms the substrate.9. The substrate of claim 1 , wherein the substrate has a geometric surface area of at least about 8 claim 1 ,000 m/m.10. The substrate of claim 1 , wherein catalytic loading is between about 55 g/ftand about 325 g/ft.11. The substrate of claim 1 , which creates a pressure drop of no greater than 120 Pa when gas flows ...

Catalyst and process for the production of diesel fuel from national gas, natural gas liquids, or other gaseous feedstocks

A unique process and catalyst is described that operates efficiently for the direct production of a high cetane diesel type fuel or diesel type blending stock from stochiometric mixtures of hydrogen and carbon monoxide. This invention allows for, but is not limited to, the economical and efficient production high quality diesel type fuels from small or distributed fuel production plants that have an annual production capacity of less than 10,000 barrels of product per day, by eliminating traditional wax upgrading processes. This catalytic process is ideal for distributed diesel fuel production plants such as gas to liquids production and other applications that require optimized economics based on supporting distributed feedstock resources. 3. A process for the production of a hydrocarbon mixture comprising; a pore diameter greater than 80 angstroms and;', 'a crush strength of greater than 3 lbs/mm and;', 'a BET surface area of greater than 110 m2/g;', 'a dispersion value between 2% and 10%,, 'reacting a feed gas that contains hydrogen and carbon monoxide with a catalyst having,'}producing a product stream comprising light gases, diesel fuel and a wax from reacting the feed gas with the supported catalyst.4. The process of claim 1 , wherein the catalyst is reduced with hydrogen at temperatures below 650 F.5. The process of claim 1 , wherein the diesel fuel fraction produced is about ⅔ of the non-gas product produced.6. The process of claim 1 , wherein the supported catalyst comprises a lobed support with more than four lobes and an effective pellet radius of less than 600 microns.7. The process of claim 4 , where all of the lobes are not equal lengths.8. The process of claim 4 , wherein the supported catalyst further comprises about 0.01 weight percent to about 2.0 weight percent of a promoter selected from the group consisting of cerium claim 4 , ruthenium claim 4 , lanthanum claim 4 , platinum claim 4 , rhenium. gold claim 4 , nickel claim 4 , or rhodium and a ...

Organosilica materials for use as adsorbents for oxygenate removal

This invention relates in certain aspects to a process for removing oxygenates from a stream, preferably a hydrocarbon stream comprising contacting an organosilica material with the hydrocarbon steam, where the organosilica material is a polymer of at least one monomer of Formula [Z 1 OZ 2 SiCH 2 ] 3 , wherein Z 1 represents a hydrogen atom, a C 1 -C 4 alkyl group, or a bond to a silicon atom of another monomer and Z 2 represents a hydroxyl group, a C 1 -C 4 alkoxy group, a C 1 -C 6 alkyl group or an oxygen atom bonded to a silicon atom of another monomer. This invention also relates to a process for polymerization comprising providing a recycle stream, wherein the recycle stream comprises one or more C 6 to C 12 conjugated or non-conjugated diene monomers and one or more C 1 to C 40 oxygenates. The recycle stream is contacted with an adsorbent bed to produce a treated recycle stream. The adsorbent bed comprises an organosilica material, which may be a mesoporous organosilica material.

Olefin polymerization catalyst system comprising mesoporous organosilica support

A catalyst system comprising a combination of: 1) an activator; 2) one or more metallocene catalyst compounds; 3) a support comprising an organosilica material, which may be a mesoporous organosilica material. The organosilica material may be a polymer of at least one monomer of Formula [Z1OZ2SiCH2]3 (I), where Z1 represents a hydrogen atom, a C1-C4 alkyl group, or a bond to a silicon atom of another monomer and Z2 represents a hydroxyl group, a C1-C4 alkoxy group, a C1-C6 alkyl group, or an oxygen atom bonded to a silicon atom of another monomer. This invention further relates to processes to polymerize olefins comprising contacting one or more olefins with the above catalyst system.

Organosilica materials and uses thereof

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

Adsorbent for heteroatom species removal and uses thereof

Adsorbent materials including a porous material support and about 0.5 wt. % to about 30 wt. % of a Group 8 metal ion are provide herein. Methods of making the adsorbent material and processes of using the adsorbent material, e.g. , for heteroatom species separation, are also provided herein.

Olefin polymerization catalyst system comprising mesoporous organosilica support

A catalyst system comprising a combination of: 1) one or more catalyst compounds comprising at least one nitrogen linkage; 2) a support comprising an organosilica material, which is a mesoporous organosilica material; and 3) an optional activator. Useful catalysts include pyridyldiamido transition metal complexes, HN5 compounds, and bis(imino)pyridyl complexes. The organosilica material is a polymer of at least one monomer of Formula [Z 1 OZ 2 SiCH 2 ] 3 (l), where Z 1 represents a hydrogen atom, a C 1 -C 4 alkyl group, or a bond to a silicon atom of another monomer and Z 2 represents a hydroxyl group, a C1-C 4 alkoxy group, a C 1 -C 6 alkyl group, or an oxygen atom bonded to a silicon atom of another monomer. This invention further relates to processes to polymerize olefins comprising contacting one or more olefins with the above catalyst system.

Olefin polymerization catalyst system comprising mesoporous organosilica support

A catalyst system comprising a combination of: 1) one or more catalyst compounds comprising at least one oxygen linkage, such as a phenoxide transition metal compound; 2) a support comprising an organosilica material, which may be a mesoporous organosilica material; and 3) an optional activator. Useful catalysts include biphenyl phenol catalysts (BPP). The organosilica material may be a polymer of at least one monomer of Formula [Z 1 OZ 2 SiCH 2 ] 3 (I), where Z 1 represents a hydrogen atom, a C 1 -C 4 alkyl group, or a bond to a silicon atom of another monomer and Z 2 represents a hydroxyl group, a C 1 -C 4 alkoxy group, a C 1 -C 6 alkyl group, or an oxygen atom bonded to a silicon atom of another monomer. This invention further relates to processes to polymerize olefins comprising contacting one or more olefins with the above catalyst system.

Olefin polymerization catalyst system comprising mesoporous organosilica support

A catalyst system comprising a combination of: 1) one or more catalyst compounds comprising at least one nitrogen linkage; 2) a support comprising an organosilica material, which is a mesoporous organosilica material; and 3) an optional activator. Useful catalysts include pyridyldiamido transition metal complexes, HN5 compounds, and bis(imino)pyridyl complexes. The organosilica material is a polymer of at least one monomer of Formula [Z1OZ2SiCH2]3(1), where Z1 represents a hydrogen atom, a C1-C4alkyl group, or a bond to a silicon atom of another monomer and Z2 represents a hydroxyl group, a C1-C4alkoxy group, a C1-C6 alkyl group, or an oxygen atom bonded to a silicon atom of another monomer. This invention further relates to processes to polymerize olefins comprising contacting one or more olefins with the above catalyst system.

Method for the production of iron-doped carbons

The invention relates to a method for producing a metal-doped supporting material containing at least one metal in the elemental form on at least one carbon-based supporting material by means of a chemical vapor deposition process in which at least one compound containing the at least one metal in oxidation state 0 is deposited on the at least one supporting material, and the at least one compound containing the at least one metal in oxidation state 0 is thermally decomposed to obtain the at least one metal in the elemental form. In said production process, the supporting material is not brought into contact with reducing compounds during and following the deposition and the decomposition. The invention further relates to a metal-doped supporting material produced according to said method as well as the use of said metal-doped supporting material for treating contaminated groundwater or wastewater.