ТЕХНОЛОГИЯ ПОВЫШЕНИЯ ТЕПЛОТВОРНОЙ СПОСОБНОСТИ УГЛЕРОДСОДЕРЖАЩЕГО ТОПЛИВА

Изобретение относится к способу увеличения теплотворной способности углеродсодержащего топлива путем каталитической гидрогенизации и трансформации при температуре 400-700°С и нормальном давлении. Способ характеризуется тем, что в качестве катализатора используют оксиды или фториды урана и их смеси с вовлечением в процесс воды в количестве, необходимом для образования моноокиси углерода СО. При сжигании продуктов гидрогенизации теплотворная способность увеличивается на 25% по сравнению с исходным топливом. 2 з.п. ф-лы, 4 табл., 3 пр., 1 ил.

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА

Изобретение относится к области производства катализатора на угольных носителях, в частности к области производства катализатора для поглощения отравляющих веществ (ОВ) и кислых аварийно-химически опасных веществ - кислых газов. Предложен способ получения катализатора, включающий приготовление водно-аммиачного раствора с содержанием каталитических добавок меди, хрома, серебра, а также триэтилендиамина общим количеством 11-20% в пересчете на катионы металлов, пропитку активного угля данным раствором, термическую обработку, при этом перед пропиткой активный уголь вакуумируют, пропитку проводят с коэффициентом 0,6-1,0 в зависимости от качества катализатора, а термическую обработку проводят при температуре 150-180°С в вибрируемом слое до полного превращения аммиачных комплексов металлов в каталитически активные по кислым аварийно-химически опасным веществам - кислым газам и отравляющим веществам (ОВ). Изобретение обеспечивает получение катализатора, имеющего высокие защитные характеристики ...

КАТАЛИЗАТОР ДЛЯ СЕЛЕКТИВНОГО ОКИСЛЕНИЯ СОЕДИНЕНИЙСЕРЫ И СПОСОБ СЕЛЕКТИВНОГО ОКИСЛЕНИЯ СОЕДИНЕНИЙ СЕРЫ ДО ЭЛЕМЕНТАРНОЙ СЕРЫ

Изобретение касается катализатора и способа селективного окисления серосодержащих соединений до элементарной серы, включающего по меньшей мере один каталитически активный компонент, выбранный из групп окислов: железа, хрома, марганца, кобальта и/или никеля, и, носитель - двуокись кремния, при этом катализатор имеет удельную площадь поверхности более 20 м2/г и средний радиус пор по меньшей мере 25 , причем этот катализатор не проявляет существенной активности по отношению к реакции Клауса. 2 с. и 2 з.п. ф-лы, 13 табл.

КАТАЛИЗАТОР ПЕРЕРАБОТКИ ТЯЖЕЛЫХ НЕФТЕЙ И СПОСОБ ЕГО ПРИГОТОВЛЕНИЯ

Изобретение относится к катализатору переработки тяжелых нефтей, включающему никель и молибден, нанесенные на гамма-оксид алюминия, модифицированный хромом, содержание которого варьируется в интервале 0.01-15 мас.%. Изобретение также относится к способу приготовления заявленного катализатора, по которому гамма-оксид алюминия модифицируют путем введения добавки хрома Cr, что позволяет получить носитель состава Cr/AlO, далее фазы никеля и молибдена последовательно наносят на модифицированный носитель, сначала пропитывают предшественником молибдена Мо в избытке растворителя, после чего пропиткой вводят никель Ni, полученный катализатор состава NiMo/Cr/AlOсушат и прокаливают. Катализаторы представляют собой мезопористые материалы, обладающие относительно высокой удельной поверхностью. Технический результат - увеличение гидрокрекирующей активности катализаторов. 2 н. и 3 з.п. ф-лы, 1 табл., 5 ил.

СПОСОБ ПОЛУЧЕНИЯ ЦИКЛОГЕКСАНА

Предложен способ получения циклогексана парофазным гидрированием бензола, содержащего в качестве примесей сернистые соединения, при повышенной температуре и повышенном давлении в нескольких реакционных зонах в присутствии никель-хромового и медьсодержащего катализаторов, расположенных в различных реакционных зонах, с использованием медьсодержащего катализатора в первой по технологическому циклу реакционной зоне, с регулированием температуры в реакционной зоне, содержащей никель-хромовый катализатор, путем подачи конденсата из сепаратора в реакционную зону с последующим его испарением. Процесс проводят в трех реакционных зонах, во второй зоне используют никель-хромовый катализатор с добавкой инертных компонентов - керамических шаров при массовом соотношении никель-хромовый катализатор:керамические шары равном (60-70):(40-30), а в третьей зоне используют никель-хромовый катализатор при массовом соотношении медьсодержащий катализатор:никель-хромовый катализатор равном (20-40):(80-60), а регулирование ...

КАТАЛИТИЧЕСКОЕ ГАЗОФАЗНОЕ ФТОРИРОВАНИЕ

... 1. Способ фторирования, который содержит:- стадию активации, содержащую контактирование катализатора фторирования с потоком газа, содержащего окислитель, в течение, по меньшей мере, одного часа; и- по меньшей мере, одну реакционную стадию, содержащую взаимодействие хлорированного соединения с фторидом водорода в газовой фазе в присутствии катализатора фторирования с тем, чтобы получить фторированное соединение.2. Способ по п. 1, который содержит множество реакционных стадий, чередующихся с множеством стадий регенерации, в котором реакционные стадии содержат взаимодействие хлорированного соединения с фторидом водорода в газовой фазе в присутствии катализатора фторирования, и стадии регенерации содержат контактирование катализатора фторирования с потоком газа, содержащим окислитель.3. Способ по любому одному из пп. 1 или 2, в котором потоком газа, содержащим окислитель, стадии активации и/или стадий регенерации является кислородсодержащий газовый поток.4. Способ по любому одному из пп. 1 ...

Verfahren zur Umwandlung von Nitrilen in Amide

EXHAUST GAS CATALYST AND METHOD OF PRODUCING THE SAME

... 1445273 Exhaust gas purification catalysts KALI-CHEMIE AG 23 Jan 1974 [27 Jan 1973 30 Jan 1973 12 Oct 1973] 03210/74 Heading BIE [Also in Division C1] Heat-, thermal shock- and fracture-resistant catalysts comprise a stainless, non-sealing and heat-resistant metal structure primed with an elastic coating of aluminium silicate and coated with a catalytic layer consisting of an oxidic carrier which enhances the activity of the catalyst and one or more catalytically active metals and/or metal oxides. The structure may be of chrome-nickel steel or nickel alloy or of enamelled carbon steel in the form of a cellular body, or of wire, tape or strip coiled, corrugated or wound into a ball, tubes, bundles of tubes, rings or saddles. The primary coat may be applied as an aqueous suspension of a fibrous aluminium silicate and an inorganic binder which is dried by heating before application, from aqueous suspension of an active layer of hydrated alumina and optionally a rare earth metal oxide, or of ...

Improvements in and relating to the selective hydrogenation of butadiene

Butadiene is selectively hydrogenated in a mixture of hydrocarbons having four carbon atoms in the molecule by bringing the mixture of hydrocarbons into contact with hydrogen at elevated temperature and at atmospheric or higher pressure in the presence of a catalyst consisting essentially of unsupported partially reduced mixed oxides of copper and chromium. The process is carried out at a temperature in the range 200-270 DEG C. and at a pressure between atmospheric and 10 atmospheres. The preferred molecular ratio of hydrogen to butadiene is 2 : 1. The copper to chromium content of the catalyst should be in the molecular proportion of about 0.5 : 1 to 1 : 1. It is advantageous to incorporate a small amount of magnesium, for example about 0.04-0.05 gram-molecule per gram-molecule of chromium. The catalyst may conveniently be prepared by treating a solution of copper nitrate and chromium trioxide in equimolecular proportions with ammonia to precipitate hydroxy-ammonium chromate. The precipitate ...

Process for the catalytic oxidation of formaldehyde

Small quantities of formaldehyde in air are converted into carbon dioxide and water by passage over a catalyst containing copper (II) oxide and/or cobalt (II) oxide. The catalyst may also contain chromic oxide, the weight ratio of Cr to Cu or Co being 0.1-1 to 1. The temperature may be 150-250 DEG C. or lower. The rate of flow of air may be 500-15,000 Nm3 per m3 of catalyst per hour. The catalyst may follow, precede, or be mixed with other catalysts suitable for the oxidation of organic compounds to prevent the formation of formaldehyde.

Catalyst compositions, their method of formulation and combustion processes using the catalyst compositions

The catalytic compositions comprise a catalytically active material which is homogeneously interspersed throughout a monolithic structure of ceramic composition. The composition is shaped into a unitary monolith which is employed as the catalyst structure. In the method the active material or materials are admixed with a ceramic material, which can be either active or inactive, in finely divided form and then shaped into the monolithic structure. The catalytic compositions are used with reactants in a combustion process.

NONOXIDATIVE DEHYDROGENATION PROCESS

PROCEDURE AND DEVICE FOR THE OXIDATION OF CARBON MONOXIDE AND HYDROCARBONS, IN SPECIAL ONE FOR THE REDUCTION OF THE POLLUTANTS IN THE EXHAUST GASES OF MOTOR VEHICLES

CATALYST AND PROCEDURE FOR THE SELECTIVE OXIDATION FROM HYDROGEN SULFIDE TO ELEMENTARY SULFUR.

Procedures for the dehydrogenation of Monoolefinen and/or alkylated aromatic hydrocarbons and catalyst for the execution of the procedure

Chromium oxide compositions containing zinc, their preparation, and their use as catalysts and catalyst precursors

PROCESS

Method for the oxidative purification of gaseous media and all metal catalyst

NOX REDUCING CATALYTIC STRUCTURE

CATALYTIC CRACKING PROCESS

F-0197-L 17 Conversion of carbon monoxide within the regenerator of a cracking unit used to regenerate spent catalysts from the catalytic cracking of gas oil is enhanced by the addition of controlled amounts of copper chromite, cobalt chromite, or mixtures thereof. Conversion of carbon monoxide in the regenerator is accomplished while maintaining the efficiency of the cracking reaction at high levels. The amount of chromite oxidation catalyst is maintained below 500 ppm based on total cracking catalyst inventory. 0197 ...

CHROMIUM-BASED CATALYSTS AND PROCESS FOR CONVERTING HYDROCARBONS TO SYNTHESIS GAS

Processes and a new family of chromium-based catalysts for the catalytic conversion of hydrocarbons to carbon monoxide and hydrogen are disclosed. One highly active and selective catalyst system, providing greater than 95% CH4 conversion, and 97-98 % selectivity to CO and H2 at conversion-promoting conditions and high space velocity, is a chromium-containing catalyst consisting of a CoCr2O4 cubic spinel precursor dispersed in a chromium oxide matrix. The catalyst precursor is reduced to cobalt metal (in a chromium oxide matrix) in the reactant stream.

CATALYST-CONTAINING OXYGEN TRANSPORT MEMBRANE

A method is described of producing a catalyst-containing composite oxygen ion membrane and a catalyst-containing composite oxygen ion membrane in which a porous fuel oxidation layer and a dense separation layer and optionally, a porous surface exchange layer are formed on a porous support from mixtures of (Ln1-xAx)wCr1-yByO3-d and a doped zirconia. Adding certain catalyst metals into the fuel oxidation layer not only enhances the initial oxygen flux, but also reduces the degradation rate of the oxygen flux over long-term operation. One of the possible reasons for the improved flux and stability is that the addition of the catalyst metal reduces the chemical reaction between the (Ln1-xAx)wCr1-yByO3-d and the zirconia phases during membrane fabrication and operation, as indicated by the X-ray diffraction results.

CHROMIUM-RARE EARTH BASED CATALYSTS AND PROCESS FOR CONVERTING HYDROCARBONS TO SYNTHESIS GAS

Catalysts and processes for the catalytic conversion of hydrocarbons to carbon monoxide and hydrogen employing new families of chromium-rare earth based catalysts are disclosed. One highly active and selective catalyst system, providing greater than 95 % CH4 conversion, and 97-98 % selectivity to CO and H2 by a net catalytic partial oxidation reaction, is a Ce-Cr-Ni containing compound. A preferred process for the catalytic conversion of a hydrocarbon comprises contacting a feed stream comprising a methane-containing hydrocarbon feedstock and an oxygen-containing gas with a chromium-rare earth containing catalyst in a short contact time reactor maintained at partial oxidation promoting conditions effective to produce synthesis gas.

STRUCTURED IRON-BASED CATALYST FOR PRODUCING A-OLEFIN FROM SYNTHESIS GAS AND PREPARATION METHOD AND USE

A structured iron-based catalyst for producing an a-olefin from a synthesis gas and a preparation method and use. The catalyst comprises an active component iron, auxiliary agents and a carrier, wherein the auxiliary agents comprise a first auxiliary agent which is a transition metal or a transition metal oxide and a second auxiliary agent which is a metal oxide. The content of the active component iron is 50.0%-99.8%, the content of the first auxiliary agent is 0-5.0%, the content of the second auxiliary agent is 0-10% and the balance is the carrier which is silicon dioxide. A precursor of the active component iron, a precursor of the first auxiliary agent and the carrier silicon dioxide are made into mono-dispersed particles using a heat dispersing method, and then impregnated with a solution of a precursor of the second auxiliary agent to obtain the structured iron-based catalyst. The above-mentioned structured iron-based catalyst is used for producing an a-olefin from a synthesis gas ...

Elément composite stratifié perméable pour traitements chimiques et physiques

COMPOSITION CATALYTIQUE, PROCEDE POUR SA PREPARATION, ET UTILISATION DE CETTE COMPOSITION CATALYTIQUE.

Verfahren zur Herstellung von Katalysatoren

Verfahren zur Herstellung von Katalysatoren

Verfahren zur Reinigung geringe Mengen Formaldehyd enthaltender Abluft

Method for preparing butadiene with excellent catalyst reproducibility

MANUFACTURE OF UNSATURATED ALIPHATIC ALCOHOLS

PERMEABLE SUPPORTS

PROCEDE DE SYNTHESE D'AMINES PRIMAIRES A PARTIR D'ESTERS

L'INVENTION CONCERNE UN PROCEDE DE SYNTHESE D'AMINES PRIMAIRES A LONGUE CHAINE, PAR REACTION D'AMMONIAC, D'HYDROGENE ET D'ESTERS D'ACIDES CARBOXYLIQUES. LA REACTION EST CONDUITE EN PRESENCE DE CATALYSEURS SPECIFIQUES CONSTITUES D'OXYDE DE TITANE ET DE METAUX ACTIFS, CUIVRE OU CUIVRE ET CHROME, ASSOCIES AU COBALT, SOUS DES PRESSIONS DE 50 A 100 BARS.

Improvements with the manufacture of aldehydes and alcohols

CATALYST COMPOSITION FOR USE IN THE GAS PHASE OXIDATION OF CARBON MONOXIDE AND HYDROCARBONS

COMPOSITION INCLUDING/UNDERSTANDING OF the PARTICLES Of MAGNETIC ALLOYS USEFUL TO PREPARE MAGNETIZABLE SOLID COMPOSITIONS, AND PROCEEDED FOR ITS OBTAINING

Cracking of hydrocarbons with septechlorite catalysts

PROCESS OF DEHYDROGENATION NON-OXYDANTE

Method of preparation of fluorinated hydrocarbons

PROCEEDED OF REDUCTION IN the NITROGEN PROTOXIDE OF EXHAUST FUMES OF MOTOR VEHICLE

SUPPORT OF CATALYST, IN PARTICULAR OF CATALYST OF POST-COMBUSTION AND MANUFACTORING PROCESS OF THIS SUPPORT

NICKEL?FREE, ALL METAL, CATALYST ELEMENT

PROCESS FOR PURIFYING EXHAUST GASES FROM MOTOR VEHICLES AND INDUSTRIAL INSTALLATIONS AND CATALYST FOR THEIR PRODUCTION/

CATALYTIC COMPOSITIONS THEIR PRODUCTION AND THEIR USE

합성 가스로부터 알파-올레핀 생산용 구조적인 철-기반 촉매, 이의 제조 방법 및 이의 사용

... 합성 가스로 부터의 알파-올레핀 생산용 구조적인 철-기반 촉매, 제조 방법, 및 용도. 상기 촉매는 활성 성분 철, 보조제 및 캐리어를 포함하며, 상기 보조제는 전이 금속 또는 전이금속 산화물인 제1 보조제 및 금속 산화물인 제2 보조제를 포함한다. 상기 활성 성분 철의 함량은 50.0% 내지 99.8%, 상기 제1 보저제의 함량은 0 내지 5.0%, 상기 제2 보조제의 함량은 0 ~10%이며, 잔량(balance)는 실리콘 이산화물인 캐리어이다. 상기 활성 성분 철의 전구체, 상기 제1 보조제의 전구체 및 상기 캐리어 실리콘 이산화물은 열 분산 방법을 이용하여 단분산 입자로 만들어지고, 다음으로 제2 보조제의 전구체 용액으로 침액되어 구조적인 철-기반 촉매를 수득한다. 전술한 구조적인 철-기반 촉매는 합성 가스로부터의 알파-올레핀 생산에 사용된다. 단분산된 구조적인 철-기반 촉매는 알파-올레핀 생성에 적합한 활성 중심을 생성할 수 있어서 좋은 선택성을 갖는다 ...

METHODS TO PREPARE A POLYMERIZATION CATALYSER

Steam dealkylation with hydrogen treated catalyst of groups I, VI B, VIII

Alkylaromatic hydrocarbons are dealkylated with steam in the presence of catalyst (typically containing oxides of nickel, potassium, chromium, and aluminum) which has been hydrogen-treated at high temperature.

Spinel dehydrogenation catalyst

Spinels promoted with an alkali metal oxide and vanadium, oxide are useful catalysts for the dehydrogenation of hydrocarbons to the corresponding more unsaturated hydrocarbons and result in an improved catalyst.

REJUVENABLE CERAMIC EXHIBITING INTRAGRANULAR POROSITY

A cermet catalyst material, including a spinel matrix defining a spinel grain and a plurality metal particles embedded in and on the surface of the spinel grain. When the spinel grain is in a first oxidizing atmosphere and at a temperature above about 800 degrees Celsius the metal particles are absorbed into the spinel matrix in the form of metal cations. When the grain is in an second, less oxidizing atmosphere and at a temperature below about 1100 degrees Celsius the metal cations emerge from the spinel matrix to yield a plurality of metal particles adhering to the spinel grain or residing in intragranular pores.

ПОЛУЧЕНИЕ ЭТАНОЛА ИЗ УКСУСНОЙ КИСЛОТЫ С ИСПОЛЬЗОВАНИЕМ КОБАЛЬТОВОГО КАТАЛИЗАТОРА

Настоящая заявка относится к способу селективного и прямого образования этанола из уксусной кислоты, в котором приводят в контакт поток сырья, содержащий уксусную кислоту и водород в газообразной форме, при температуре от 200°C до 300°C с катализатором гидрирования, содержащим кобальт и второй металл на каталитическом носителе, где кобальт присутствует в количестве от 0,1% мас. до 20% мас., и где второй металл выбирают из группы, состоящей из палладия, платины и хрома. 14 з.п. ф-лы, 10 пр.

СПОСОБ ПОЛУЧЕНИЯ МЕДЬЦИНКХРОМАЛЮМИНИЕВОГО КАТАЛИЗАТОРА

Изобретение относится к получению катализаторов на основе соединений меди, цинка, алюминия и хрома для низкотемпературной конверсии оксида углерода водяным паром, катализатор может быть использован для низкотемпературного синтеза метанола, процессов гидрирования нитробензола, дегидрирования циклогексанола в циклогексанон в производстве капролактама. Способ получения медьцинкхромалюминиевого катализатора осуществляют путем смешения раствора аммиачно-карбонатного комплекса меди с соединениями цинка и алюминия с последующими сушкой, прокаливанием и таблетированием катализаторной массы, отличающийся тем, что в аммиачно-карбонатный раствор комплекса меди постепенно вводят оксид цинка и порошок оксида алюминия γ-модификации с тониной помола менее 100 мкм, полученную суспензию с соотношением твердое:жидкое, равным 1,0:(12,0-15,0), нагревают при перемешивании в интервале температур 60-90°С до получения массы с соотношением твердое:жидкое, равным 1,0:(0,01-0,5), затем вводят хромовый ангидрид или ...

СПОСОБ ПРИГОТОВЛЕНИЯ КАТАЛИЗАТОРА ГЛУБОКОГО ОКИСЛЕНИЯ И СПОСОБ КАТАЛИТИЧЕСКОГО СЖИГАНИЯ ИЛОВОГО ОСАДКА КОММУНАЛЬНЫХ ОЧИСТНЫХ СООРУЖЕНИЙ

Изобретение относится к области разработки способов приготовления катализаторов глубокого окисления и способам сжигания иловых осадков коммунальных очистных сооружений. Описан способ приготовления катализатора, в котором гранулы катализатора получают методом жидкостного формования пластифицированной массы, состоящей из активного компонента на основе оксидов переходных металлов или их смеси с содержанием их не менее 50 мас.% (в пересчете на сухое вещество), гидроксида алюминия, кислоты пептизатора и воды, в раствор аммиака через слой углеводородной жидкости, сушкой и прокаливанием, при этом получают сферический катализатор, содержащий в качестве оксидного носителя оксид алюминия в количестве не более 50 мас.%, а в качестве активного компонента Fe2O3в количестве 48-75 мас.%, а также CuO в количестве 0 мас.%, 2-3 мас.%, 3,5-6 мас.% и/или Mn2O3и/или Co2O3и/или Cr2O3в количестве 2-10 мас.%. Описан способ сжигания илового осадка коммунальных очистных сооружений в кипящем слое катализатора, полученного ...

КАТАЛИЗАТОР ГЛУБОКОГО ОКИСЛЕНИЯ И СПОСОБ КАТАЛИТИЧЕСКОГО СЖИГАНИЯ ИЛОВОГО ОСАДКА КОММУНАЛЬНЫХ ОЧИСТНЫХ СООРУЖЕНИЙ

Изобретение относится к катализатору для сжигания илового осадка коммунальных очистных сооружений, состоящему из оксидного носителя оксида алюминия в количестве не более 50 мас. %, активного компонента Fe2O3в количестве 48-75 мас. %, а также CuO в количестве 0 мас. %, 2-3 мас. %, 3,5-6 мас. %, и/или Mn2O3,и/или Co2O3, и/или Cr2O3в количестве 2-10 мас. %, а также к способу сжигания илового осадка коммунальных очистных сооружений в кипящем слое катализатора с использованием данного катализатора. 2 н.п. ф-лы, 8 пр., 1 табл., 1 ил.

ПОЛУЧЕНИЕ ЭТАНОЛА ИЗ УКСУСНОЙ КИСЛОТЫ С ИСПОЛЬЗОВАНИЕМ КОБАЛЬТОВОГО КАТАЛИЗАТОРА

... 1. Способ селективного и прямого образования этанола из уксусной кислоты, в котором приводят в контакт поток сырья, содержащий уксусную кислоту и водород в газообразной форме, при температуре от 200°С до 300°С с катализатором гидрирования, содержащим кобальт и второй металл на каталитическом носителе, где кобальт присутствует в количестве от 0,1 мас.% до 20 мас.%, и где второй металл выбирают из группы, состоящей из палладия, платины и хрома. ! 2. Способ по п.1, где данный каталитический носитель выбирают из группы, состоящей из оксида кремния, оксида алюминия, силиката кальция, углерода, оксида циркония и оксида титана. ! 3. Способ по п.1, где данный второй металл представляет собой палладий. ! 4. Способ по п.3, где содержание кобальта составляет от 4 до 12 мас.%, а содержание палладия составляет от 0,5 до 2 мас.%, и данный каталитический носитель представляет собой графит. ! 5. Способ по п.1, где данный второй металл представляет собой платину. ! 6. Способ по п.5, где содержание кобальта ...

КАТАЛИТИЧЕСКОЕ ГАЗОФАЗНОЕ ФТОРИРОВАНИЕ

Изобретение относится к способу фторирования, который содержит: стадию активации, содержащую контактирование катализатора фторирования с потоком газа, содержащего окислитель, в течение, по меньшей мере, одного часа; и по меньшей мере, одну реакционную стадию, содержащую взаимодействие хлорированного соединения с фторидом водорода в газовой фазе в присутствии катализатора фторирования с тем, чтобы получить фторированное соединение. При этом поток газа, содержащий окислитель, не содержит фторид водорода. Способ позволяет добиваться увеличенной степени конверсии и/или селективности и является эффективным в течение длительного периода времени. 19 з.п. ф-лы, 2 табл., 7 пр.

CATALYST

PROCESS FOR REDUCING OXIDES OF NITROGEN

... 1400573 Reducing nitrogen oxides in internal combustion engine exhaust gases STANDARD OIL CO 23 Aug 1972 [27 Aug 1971] 39201/72 Heading C1A [Also in Division B1] Oxides of nitrogen in an I.C.E. exhaust gas are reduced by passing the gas over a catalyst comprising 23-28 wt. per cent NiO, 5-8 wt. per cent CuO, 5-8 wt. per cent Cr 2 O 3 and 0À5-2 wt. per cent Fe 2 O 3 on an inorganic, porous, refractory support material at 500-1500‹ F., GHSV of 15,000-35,000 and an O 2 : CO ratio less than 0À6. The catalyst may also contain BaO or a platinum group metal, e.g. Pt and Pd.

Process for the preparation of chromium silicate-type catalysts

A chromium silicate type catalyst is prepared by heating together silica, an alkali metal chromate and a catalytic quantity (e.g. 0.1-0.5 per cent. calculated as oxide) of a compound of an element of the group consisting of iron and the elements of Group 2 of the Periodic Table. Preferably 0.5-4 parts by weight of the chromate are used for 6 parts of silica, and heating is carried out at a temperature not below 800 DEG C. The products may be regarded as solutions of chromium sesquioxide in silica, as chromium silicates, or as complex alkali-metal silicates. A compound having the formula M2O.Cr2O3, (SiO2)5 is claimed. Examples describe heating mixtures containing ground sand or quartz, sodium chromate, calcium chloride and ferric chloride. Silica may be added to an aqueous solution of the other substances and the mixture evaporated to dryness. Copper, zinc, bismuth, magnesium, titanium, vanadium, manganese, molybdenum or tungsten as oxides or borates may be added as promoters. The catalyst ...

HYDROCARBON CONVERSION CATALYSTS AND PRECURSORS

... 1495601 Synthetic septechlorites NL INDUSTRIES Inc 7 Jan 1975 [7 Jan 1974] 690/75 Heading C1A [Also in Division Bl] A synthetic septechlorite being a 1:1 trioctahedral phyllosilicate with equal degrees of trivalent ion substitution in both octahedral and tetrahedral layers is prepared having the following chemical composition (6 - x)A2+O.xB 2 3+O 3 (4-x)SiO 2 .(4-y)H 2 OyHF where A is Ni, Mg, Co, Fe2+, Cu2+, Mn2+, Zn or mixtures thereof B is Al, Cr, Fe3+ or mixtures thereof O#x# O#y#1 x+y#0À1 O#Co#5À75 O#Fe2+#5À25 O#Zn#4 4#(Ni + Mg + Co + Fe2+ + Cu + Mn + Zn)#6 O#Cu#0À5 O#Mn#0À5 (Cr+Ni+Co+Cu+Mn)>0À1 O#Fe3+#1. In an example Ni-Al septechlorites are prepared from a feed of formulation (6 - x)NiCl 2 À2xAlCl 3 À(4 - x)SiO 2 À(12 + 4x)NaOH the SiO 2 being in the form of polysilicic acid. The components are placed in a pressure vessel with 250 moles H 2 O and reacted at 350‹ C. for 6 hr. The septechlorites are calcined ...

Process for catalytic hydrodesulfurization of petroleum hydrocarbons and catalysts therefor

A hydrodesulphurization catalyst supported on a porous carrier, e.g. alumina, contains molybdenum, preferably 4-16% (wt.) and at least two of the metals iron, nickel and cobalt as their oxides, sulphides or combinations of oxides or sulphides with molybdenum oxide or sulphide, the atomic ratios of each metal to molybdenum being less than 0.4 and the sum of the atomic ratios of the metals to molybdenum being less than 0.8. One member of the metals can be present in a substantially smaller atomic ratio to molybdenum than the other, for example, in a catalyst containing molybdenum with cobalt and nickel, the cobalt to molybdenum ratio is 0.01 to 0.05 and the nickel to molybdenum range is 0.1 to 0.2 The catalysts are used to reduce the sulphur content of sulphur containing hydrocarbons, for example, furnace oils, naphthas, cracking charge stock, shale oils, coke oven oils or residual-containing hydrocarbons, such as whole crude or reduced crude, by contacting the hydrocarbon with hydrogen in ...

HYDROCARBON SYNTHESIS CATALYST PREPARATION

Hydrocarbon synthesis catalyst preparation

A process for preparing a catalyst for converting syngas to middle distillates which comprises kneading and/or impregnating cobalt and another metal (Zr, Ti, Cr) onto a carrier (SiO2, Al2O3, SiO2/Al2O3) in such a way that L and S satisfy the relation: (3+4R)>(L/S)>(0.3+0.4R), wherein L=the total quantity of cobalt present on the catalyst, expressed as mg Co/ml catalyst; S=the surface area of the catalyst, expressed as M2/ml catalyst; and R=the weight ratio of the quantity of cobalt deposited on the catalyst by kneading to the total quantity of cobalt present on the catalyst.

Catalyst compostions, their method of formation and combustion processes using the catalyst compositions

The catalytic compositions comprise a catalytically active material which is homogeneously interspersed throughout a monolithic structure of ceramic composition. The composition is shaped into a unitary monolith which is employed as the catalyst structure. In the method the active material or materials are admixed with a ceramic material, which can be either active or inactive, in finely divided form and then shaped into the monolithic structure. The catalytic compositions are used with reactants in a combustion process.

PROCESS FOR CONVERTING A NITRILE TO THE CORRESPONDING AMIDE

... 1294171 Oxide catalyst DOW CHEMICAL CO 14 Jan 1970 [16 Jan 1969 23 June 1969] 1894/70 Heading B1E [Also in Division C2] A catalyst comprising reduced copper oxide, reduced copper - chromium oxide, reduced copper-molybdenum oxide, or a mixture thereof is prepared by reducing the appropriate oxides with elemental hydrogen, suitably at a temperature of from 50 to 500‹C. Examples describe the preparation of a reduced copper oxide-chromium oxide catalyst in which the starting oxides are obtained by reacting ammonium chromate with copper chloride. The catalysts are used for converting a nitrile to the corresponding amide. The Examples all relate to Cu plus Cr. In Example 5, barium is also present.

Improvements in or relating to Catalytic Oxidation of Exhaust Gases

... 1,168,075. Treating exhaust gases. PETER SPENCE & SONS Ltd. Sept. 23, 1966 [Sept. 24, 1965], No. 42526/66. Heading FIB. [Also in Division C1] Exhaust gases of those emanating from the exhaust system of an I. C. engine are oxidized e. g. to CO2 + H2O in the presence of a catalyst composition comprising a substantially homogeneous mixture of gamma-Al2O3 and at least two heavy metal oxides, one being chromium oxide and the other being an oxide of Ti, V, Mu, Fe, Co, Ni, Cu or Zn, such that the proportion of heavy metal oxides in the composition is more than 50 cwt. %. Comparative examples disclose the conversion of hydrocarbons and carbon monoxide under standardized conditions.

METHOD FOR TREATING AMMONIA-CONTAINING GASES

... 1476347 Ammonia oxidation catalysts SUMITOMO CHEMICAL CO Ltd 22 Oct 1974 [24 Oct 1973 25 April 1974] 45641/74 Heading B1E [Also in Division C1] A catalyst for use in the removal of NH 3 from gases has a general formula: wherein A is at least one of Sn, Sb, V, Co, Ag, Zn, Ni, Ti, Mo, W, S, P, B, Ge or Zr; x is 4-12; y is 0.2-8 and z is 6.2-42. The ratio of x:y is preferably in the range of 11.5:0.5 to 6:6. The catalyst may comprise the catalyst components alone in the form of granules, tablets or extrusion moulded products or may be supported on a carrier such as activated alumina, alpha-alumina, silica gel, aluminosilicate, diatomaceous earth or silicon carbide. The catalyst may be made by reacting the appropriate water-soluble salts, a variety of suitable salts being specified. Alternatively, the catalysts may be made by mixing an aqueous solution of chromic anhydride with an aqueous solution of the water-soluble starting materials. The catalyst is preferably dried at 60-250‹ until the ...

METHOD FOR PURIFYING GASES FROM SULPHUROUS COMPOUNDS

KUPFERCHROMITKATALYSATORUND PROCEDURES FOR THE PRODUCTION OF THE SAME

Catalyst for the production from hydrogen from kohlenmonoxydhaltigen gases and procedure to its production

CATALYST PRODUCTION.

PROCEDURE AND DEVICE FOR THE OXIDATION OF CARBON MONOXIDE AND HYDROCARBONS, IN SPECIAL ONE FOR THE REDUCTION OF THE POLLUTANTS IN THE EXHAUST GASES OF MOTOR VEHICLES

Procedure for the production of spherical catalysts

MANUFACTURE OF UNSATURATED ALIPHATIC ALCOHOLS

Catalyst, use thereof and process for preparation thereof

MANUFACTURE OF UNSATURATED ALIPHATIC ALCOHOLS

Ethanol production from acetic acid utillizing a cobalt catalyst

Hydrothermal hydrocatalytic treatment of biomass using water tolerant catalysts

A method of hydrothermal hydrocatalytic treating biomass is provided. Lignocellulosic biomass solids is provided to a hydrothermal digestion unit in the presence of a digestive solvent, and a supported hydrogenolysis catalyst containing (a) sulfur, (b) Mo or W, and (c) Co, Ni or mixture thereof, incorporated into an alumina support, which support is predominantly alpha alumina; (ii) heating the lignocellulosic biomass solids and digestive solvent in the presence of hydrogen, and supported hydrogenolysis catalyst thereby forming a product solution containing plurality of oxygenated hydrocarbons, said alumina support having a specific surface area of up to 30 m2/g and said catalyst retaining a crush strength of at least 50% after being subjected to an aqueous phase stability test compared with before the aqueous phase stability test or a crush strength of at least 0.25 kg after being subjected to an aqueous phase stability test.

PREPARATION OF SATURATED PRIMARY AMINES

... - 13 - O.Z.0050/36947 Saturated primary amines are prepared by reacting a nitrile with hydrogen at elevated temperatures and under superatmospheric pressure in the presence of ammonia by a process in which a molded catalyst material as used which has an indentation hardness of >300 kp/cm2 and contains metallic cobalt and/or nickel particles, obtained from cobalt oxide and/or nickel oxide particles containing less than 0.1% by weight of alkali metal oxides and/or alkaline earth metal oxides by reduction with hydrogen at <500.degree.C, and a lubricant.

CATALYST PREPARATION

ARTICULATED HELIX SUPPORT

DEHYDROGENATION CATALYST

PROCESS FOR THE CONVERSION OF METHOXYLATED AROMATIC COMPOUNDS TO SIMPLE AROMATIC COMPOUNDS

Hydrotreating catalysts and processes useful for the conversion of methoxylated aromatic compounds to simple aromatic compounds are provided. The catalysts comprise transition metal selected from the group consisting of Group 8 metals, Group 9 metals, Group 10 metals, Group 11 metals, and mixtures thereof, and catalyst support selected from the group consisting of shape-selective zeolite, silica, titania, zirconia, and mixtures thereof.

PROCESS FOR THE CONVERSION OF METHOXYLATED AROMATIC COMPOUNDS TO SIMPLE AROMATIC COMPOUNDS

Hydrotreating catalysts and processes useful for the conversion of methoxylated aromatic compounds to simple aromatic compounds are provided. The catalysts comprise transition metal selected from the group consisting of Group 8 metals, Group 9 metals, Group 10 metals, Group 11 metals, and mixtures thereof, and catalyst support selected from the group consisting of shape-selective zeolite, silica, titania, zirconia, and mixtures thereof.

ACTIVATION AND REGENERATION OF FLUORINATION CATALYSTS

A fluorination catalyst such as a chromium oxide-based fluorination catalyst may be activated or reactivated by contacting the catalyst. with a source of reactive fluorine, for example nitrogen trifluoride (NF3) or fluorine (F2). Fluorinated compounds may be prepared by the gas phase reaction of hydrogen fluoride (HF) with various substrates such as chlorinated compounds. A number of metal oxide-based catalysts have been developed for this purpose.

Method for producing higher hydridosilane

The invention relates to a method for producing higher hydridosilane wherein at least one lower hydridosilane and at least one heterogeneous catalyst are brought to reaction, wherein the at least one catalyst comprises Cu, Ni, Cr and/or Co applied to a carrier and/or oxide of Cu, Ni, Cr and/or Co applied to a carrier, the hydridosilane that can be produced according to said method and use thereof.

Process of dehydrogenation and nonaromatic hydrocarbon deshydrocyclisation

Improvements with catalysts and the catalytic processes

Vehicle exhaust purifier - for catalytic reduction of oxides of nitrogen

PROCEDE DE DESHYDROGENATION SANS OXYDATION ET COMPOSITION CATALYTIQUE POUR LA MISE EN OEUVRE DE CE PROCEDE

LA PRESENTE INVENTION CONCERNE UN PROCEDE POUR LA PREPARATION D'UN COMPOSE DONT LA FORMULE EST R-CHCH, PAR LA DESHYDROGENATION SANS OXYDATION D'UN COMPOSE DONT LA FORMULE EST R-CH-CH, R REPRESENTANT UN GROUPE PHENYLE, ALCOYLE OU ALCENYLE. CE PROCEDE COMPREND LE PASSAGE D'UN MELANGE D'UN COMPOSE DONT LA FORMULE EST R-CH-CH, R REPRESENTANT UN GROUPE PHENYLE, ALCOYLE OU ALCENYLE, ET DE VAPEUR SURCHAUFFEE, A LA TEMPERATURE DE DESHYDROGENATION, SUR UN CATALYSEUR QUI EST UNE SPINELLE, CONTENANT UN OXYDE DE METAL ALCALIN ET DE L'OXYDE DE VANADIUM SERVANT DE PROMOTEURS. APPLICATION DANS LA FABRICATION DE STYRENE.

ELEMENT FOR FILTERING AND/OR PURIFICATION OF HOT GAS, AND ITS MANUFACTURING METHOD.

Steam dealkylation catalyst - typically contg. oxides of nickel, potassium, chromium and aluminium

PROCESS FOR REDUCING OXIDES OF NITROGEN

Catalyst carrier having high strength and thermal stability - consisting of fused mixt. of alumina with oxides of other metals

CATALYSTS FOR the CONTROL OF the EMISSIONS Of EXHAUST OF DIESEL

PROCESS FOR THE MANUFACTURE OF A CATALYTIC REACTOR

CATALYST PREPARED BY GRINDING REAGENT

METHOD FOR PREPARATION OF DIPHENYLAMINES

Fischer-tropsch synthesis catalyst, preparation and application thereof

A micro-spherical Fe-based catalyst for a slurry bed Fischer-Tropsch synthesis (FTS) comprises Fe as its active component, a transitional metal promoter M, a structure promoter S and a K promoter. The transitional metal promoter M is one or more selected from the group consisting of Mn, Cr and Zn, and the structure promoter S is SiO 2 and/or Al 2 O 3 . The weight ratio of the catalyst components is Fe: transitional metal promoter: structure promoter: K=100:1-50:1-50:0.5-10. Preparation method of the catalyst comprises: adding the structure promoter S into a mixed solution of Fe/M nitrates, then co-precipitating with ammonia water to produce a slurry, filtering and washing the slurry to produce a filter cake, adding the required amount of the K promoter and water to the filter cake, pulping and spray drying, and roasting to produce the micro-spherical Fe-based catalyst for the slurry bed Fischer-Tropsch synthesis. The catalyst has good abrasion resistance and narrow particle size distribution, furthermore, it has high conversion capability of synthesis gas, good product selectivity and high space time yield, and the catalyst also can be used for the slurry bed Fischer-Tropsch synthesis in a wide temperature range.

Catalyst for Removing Nitrogen Oxides

The present invention is to provide a catalyst for removing nitrogen oxides which is capable of keeping sufficient denitrification performance, i.e., a high removal rate of nitrogen oxides in exhaust gas having a high NO 2 content especially under conditions where the ratio of NO 2 /NO in exhaust gas is 1 or higher, a catalyst molded product therefor, and an exhaust gas treating method. The catalyst is designed for removing nitrogen oxides, which is used to denitrify exhaust gas containing nitrogen oxides having a high NO 2 content, which comprises: at least one kind of oxide selected from the group consisting of copper oxides, chromium oxides, and iron oxides as a component for reducing NO 2 to NO; and which further comprises: at least one kind of titanium oxide; at least one kind of tungsten oxide; and at least one kind of vanadium oxide as components for reducing NO to N 2 .

Methanation Reaction Methods Utilizing Enhanced Catalyst Formulations and Methods of Preparing Enhanced Methanation Catalysts

Enhanced mixed metal catalysts are provided which allow high conversions of carbon dioxide to methane, in some cases up to about 100% conversion. Methods of preparing enhanced mixed metal catalysts comprise a series of steps involving combining nickel and chromium salts with a nucleation promoter in a base environment to form a gel, allowing the gel to digest to form a solid and a mother liquor, isolating the solid, washing the solid, drying the solid, and thermally treating the solid to form a nickel-chromium catalyst. Methanation processes using the catalysts are also provided. The enhanced mixed metal catalysts provide more efficient conversion and lower operating temperatures for carbon dioxide methanation when compared to conventional methanation catalysts. Additionally, these enhanced catalyst formulations allow realization of higher value product from captured carbon dioxide.

Process for preparing higher hydridosilanes

The invention relates to a method for producing higher hydridosilane wherein at least one lower hydridosilane and at least one heterogeneous catalyst are brought to reaction, wherein the at least one catalyst comprises Cu, Ni, Cr and/or Co applied to a carrier and/or oxide of Cu, Ni, Cr and/or Co applied to a carrier, the hydridosilane that can be produced according to said method and use thereof.

Catalyst containing oxygen transport membrane

A composite oxygen transport membrane having a dense layer, a porous support layer and an intermediate porous layer located between the dense layer and the porous support layer. Both the dense layer and the intermediate porous layer are formed from an ionic conductive material to conduct oxygen ions and an electrically conductive material to conduct electrons. The porous support layer has a high permeability, high porosity, and a microstructure exhibiting substantially uniform pore size distribution as a result of using PMMA pore forming materials or a bi-modal particle size distribution of the porous support layer materials. Catalyst particles selected to promote oxidation of a combustible substance are located in the intermediate porous layer and in the porous support adjacent to the intermediate porous layer. The catalyst particles can be formed by wicking a solution of catalyst precursors through the porous support toward the intermediate porous layer.

PROCESS FOR THE PREPARATION OF CU-CR OXIDES FOR SELECTIVE OXIDATION REACTIONS

The present invention provides a process for the preparation of Cu—Cr oxides by hydrothermal synthesis method using hydrazine as a reducing agent and cetyltrimethylammonium bromide as a surfactant and these oxides are very active for selective oxidation of benzene, toluene and ethylbenzene to produce phenol, benzaldehyde and acetophenone, respectively. 1. A process for the preparation of Cu—Cr oxide as catalyst , the process comprising the steps of:{'sub': 3', '2', '2', '3', '3', '2, 'a. mixing of Cu(NO).3HO and Cr(NO).9HO to obtain a solution, wherein the molar ratio of Cu to Cr is in the range of 0.05-0.7,'}b. adding a surfactant drop wise into the solution as obtained in step (a) with constant stirring, wherein the molar ratio of Cu to surfactant in the obtained solution is in the range of 0.5 to 1.5,c. adding a reducing agent drop wise into the solution as obtained in step (b) with constant stirring to obtain a gel wherein the molar ratio of Cu to reducing agent is in the range of between 0.5 to 1.5,d. heating the gel as obtained in step (c) at temperature ranging between 30-55° C. for a period ranging between 2-4 hrs followed by heating the gel at temperature ranging between 100-200° C. hydrothermally for a period ranging between 12-30 hours to obtain solid catalyst followed by washing the solid catalyst with excess water,e. drying the solid catalyst as obtained in step (d) at 80-110° C. for a period in the range of 6-12 h.f. calcining the solid catalyst as obtained in step (e) at temperature ranging between 300-900° C. for a period of 5-12 hrs to obtain Cu—Cr oxide catalyst.2. The process according to claim 1 , wherein the surfactant used in step (b) is cetyltrimethyl ammonium bromide (CTAB).3. The process according to claim 1 , wherein the reducing agent used in step (c) is hydrazine.4. A process for single step selective oxidation of aromatic compounds using catalyst of claim 1 , wherein the process comprises the steps of:{'claim-ref': {'@idref': 'CLM-00001 ...

CATALYST, ELECTRODE, FUEL CELL, GAS DETOXIFICATION APPARATUS, AND METHODS FOR PRODUCING CATALYST AND ELECTRODE

Provided are a catalyst, an electrode, a fuel cell, a gas detoxification apparatus, and the like that can promote a general electrochemical reaction causing gas decomposition or the like. A catalyst according to the present invention is used for promoting an electrochemical reaction and is chain particles formed of an alloy particles containing nickel (Ni) and at least one selected from the group consisting of iron (Fe), cobalt (Co), chromium (Cr), tungsten (W), and copper (Cu). 1. A catalyst used for promoting an electrochemical reaction , comprising:an alloy containing nickel (Ni) and at least one selected from the group consisting of iron (Fe), cobalt (Co), chromium (Cr), tungsten (W), and copper (Cu).2. The catalyst according to claim 1 , being chain particles in which particles that have a diameter of 0.5 μm or less and are formed of the alloy are connected to form an elongated shape.3. The catalyst according to claim 2 , wherein the chain particles have branches and form dendritic chain particles in which the branched chain particles are intertwined.4. The catalyst according to claim 1 , wherein the alloy contains 0.5% or less by weight of titanium (Ti).5. The catalyst according to claim 1 , being a woven fabric formed of fibers of the alloy or a metal-fiber woven fabric including a plated layer of the alloy.6. The catalyst according to claim 1 , being a porous plated body formed of the alloy or a porous plated body including a plated layer of the alloy.7. The catalyst according to claim 1 , being particles that are formed of the alloy and have an average diameter of 100 μm or less.8. The catalyst according to claim 1 , being present with a solid electrolyte and disposed in a form of a film of the alloy or a deposit of the alloy so as to cover a surface of the solid electrolyte.9. The catalyst according to claim 1 , wherein oxygen is bonded to a surface of the alloy or the alloy is covered with an oxide layer.10. An electrode formed by sintering the catalyst ...

Esterifying an ethanol and acetic acid mixture to produce an ester feed for hydrogenolysis

Disclosed herein are processes for alcohol production by hydrogenating acetic acid to obtain a mixture of ethanol and acetic acid, esterifying the mixture to produce an esterification product and reducing the esterification product. The mixture may provide a sufficient amount of ethanol and acetic acid for esterification and reduces the need for additional acetic acid and/or ethanol. This may reduce the recycle of ethanol in the hydrogenolysis process and improve ethanol productivity.

Process for the Hydrotreatment of Vegetal Materials

The present invention relates to a process for the hydrotreatment of a vegetal biomass. Specifically, the present invention relates to a process for the hydrotreatment of a vegetal biomass comprising: a) subjecting said vegetal biomass to a hydrotreatment in a first reactor, said hydrotreatment comprises contacting said vegetal biomass in an aqueous medium and a metal oxide, a mixed metal oxide, or a metal-metalloid oxide catalyst comprising at least 35% by weight of metal oxide, mixed metal oxide, or metal-metalloid oxide relative to the total weight of the catalyst, with hydrogen at a pressure in the range of 10 to 400 bar and at a temperature in the range of 50° C. to 300° C. until a predetermined level of the hydrotreatment of said biomass is obtained and wherein the metal oxide, a mixed metal oxide, or a metal-metalloid oxide catalyst comprises nickel. Further, the present invention relates to a metal oxide, mixed metal oxide or metal-metalloid oxide catalyst. Furthermore, the present invention relates to the use of the catalyst. 1. Process for the hydrotreatment of a vegetal biomass comprising:a) subjecting said vegetal biomass to a hydrotreatment in a first reactor, said hydrotreatment comprises contacting said vegetal biomass in an aqueous medium and a metal oxide, a mixed metal oxide, or a metal-metalloid oxide catalyst comprising at least 35% by weight of metal oxide, mixed metal oxide, or metal- metalloid oxide relative to the total weight of the catalyst, with hydrogen at a pressure in the range of 10 to 400 bar and at a temperature in the range of 50° C. to 300° C. until a predetermined level of the hydrotreatment of said biomass is obtained and wherein the metal oxide, a mixed metal oxide, or a metal-metalloid oxide catalyst comprises nickel.2. Process according to claim 1 , wherein the process further comprises:b) subjecting the mixture of step a) to a second hydrotreatment in a second reactor and contacting the hydrotreated vegetal biomass in an ...

Catalyst for hydrocarbon steam cracking, method of preparing the same and method of preparing olefin by using the same

The present invention relates to a catalyst for hydrocarbon steam cracking, a method of preparing the same, and a method of preparing olefin by the hydrocarbon steam cracking by using the catalyst, and more specifically, to a catalyst for hydrocarbon steam cracking for preparing light olefin including an oxide catalyst (0.5≦j≦120, 1≦k≦50, A is transition metal, and x is a number satisfying conditions according to valence of Cr, Zr, and A and values of j and k) represented by CrZr j A k O x , wherein the composite catalyst is a type that has an outer radius r 2 of 0.5 R to 0.96 R (where R is a radius of a cracking reaction tube), a thickness (t; r 2 −r 1 ) of 2 to 6 mm, and a length h of 0.5 r 2 to 10 r 2 , a method of preparing the same, and a method of preparing light olefin by using the same.

Dehydrogenation of alkanols to increase yield of aromatics

The present invention provides methods, reactor systems, and catalysts for increasing the yield of aromatic hydrocarbons produced while converting alkanols to hydrocarbons. The invention includes methods of using catalysts to increase the yield of benzene, toluene, and mixed xylenes in the hydrocarbon product.

One-Step Synthesis of Monodisperse Transition Metal Core-Shell Nanoparticles with Solid Solution Shells

Methods of forming monodispersed core-shell nanoparticles are provided. A cobalt(II)-ligand component, a metal(II)-ligand component, an organic reducing agent, and a capping agent can be added to an organic solvent to form a reaction mixture. The reaction mixture is then heated to a dissolving temperature while under a gas (e.g., including methane) such that the reaction mixture becomes a reaction solution while stirring at the dissolving temperature. The reaction solution is then be heated to a reaction temperature (e.g., about 200° C. or more) while under the gas to form the core-shell nanoparticles, and the core-shell nanoparticles can be collected from the reaction solution. 1. A method of forming monodispersed core-shell nanoparticles , the method comprising:adding a cobalt(II)-ligand component, a metal(II)-ligand component, an organic reducing agent, and a capping agent to an organic solvent to form a reaction mixture, wherein the metal(II)-ligand comprises a metal(II) selected from the group consisting of copper(II), iron(II), chromium(II), scandium(II), nickel (II), zirconium (IV), and mixtures thereof;heating the reaction mixture to a dissolving temperature while under a gas, wherein the reaction mixture becomes a reaction solution while stirring at the dissolving temperature, and wherein the gas comprises methane;heating the reaction solution to a reaction temperature while under the gas to form the core-shell nanoparticles, wherein the reaction temperature is about 200° C. or more; andcollecting the core-shell nanoparticles from the reaction solution.2. The method as in claim 1 , further comprising:after collecting the core-shell nanoparticles, dispersing the core-shell nanoparticles in a solvent.3. The method as in claim 1 , wherein the metal(II)-ligand component comprises a copper(II)-ligand.4. The method as in claim 3 , wherein the copper(II)-ligand comprises copper(II)-acetylacetonate.5. The method as in claim 3 , wherein the core-shell nanoparticles ...

Catalyst for the hydrogenation of unsaturated hydrocarbons and process for its preparation

The present invention relates to a catalyst for the hydrogenation of unsaturated hydrocarbons, in particular aromatics with a broad molecular weight range, a process for the production thereof and a process for hydrogenating unsaturated hydrocarbons.

METAL STRUCTURE CATALYST AND PREPARATION METHOD THEREOF

Provided are a metal structure catalyst and a method of preparing the same. Particularly, the method includes forming a metal precipitate on a metal support by contact of a mixed solution including a precursor of a metal catalyst and a precipitating agent with the metal support, and forming metal particles by thermally treating and reducing the metal precipitate formed on the metal support. The metal structure catalyst includes a metal support, a metal oxide layer formed on the metal support, and metal nanoparticles formed on the metal oxide layer. In addition, the metal nanoparticles are uniform and have enhanced binding strength. 1. A method of preparing a metal structure catalyst , comprising:forming a metal precipitate on a metal support by contact of a mixed solution including a precursor of a metal catalyst and a precipitating agent with the metal support; andforming metal particles by thermally treating and reducing the metal precipitate formed on the metal support.2. The method according to claim 1 , wherein the metal catalyst includes at least one atom selected from the group consisting of nickel claim 1 , ruthenium claim 1 , platinum claim 1 , rhodium claim 1 , ceria and zirconia.3. The method according to claim 1 , wherein a precursor solution of the metal catalyst is at least one selected from the group consisting of a metal nitrate claim 1 , a metal halide claim 1 , a metal acetate claim 1 , a metal sulfate claim 1 , a metal acetoacetate claim 1 , a metal fluoroacetoacetate claim 1 , a metal perchlorate claim 1 , a metal sulfamate claim 1 , a metal stearate claim 1 , a metal phosphate claim 1 , a metal carbonate claim 1 , a metal oxalate and a metal complex.4. The method according to claim 1 , wherein the precipitating agent is at least one selected from the group consisting of KOH claim 1 , NaOH claim 1 , ammonia claim 1 , urea claim 1 , NaCO claim 1 , and KCO.5. The method according to claim 1 , wherein the precipitating agent controls a pH of the ...

Catalytic Process for Production of Pyridine Carboxylic Acid Amides

An improved catalytic process for the production of pyridine carboxylic acid amides, by catalytic hydration reaction of pyridine nitriles with solid heterogeneous catalyst wherein the process involve effective utilization and recycling of the catalytic components, and reactants. 1. A process for producing pyridine carboxylic acid amide compounds , analogs , substituted forms , derivatives , or pharmaceutically acceptable salts , esters , prodrugs , solvates and hydrates thereof , the process comprising:a catalytic hydrolysis of pyridine nitrile compound with water in the presence of a solid heterogeneous catalyst, optionally in alcohol,wherein the catalyst, water and other reactant materials are reused and wherein the catalyst, when deactivated is regenerated and reused in the process.2. The process according to claim 1 , wherein the catalyst is selected from the group comprising oxides claim 1 , hydroxides claim 1 , carbonates claim 1 , bicarbonates claim 1 , nitrates claim 1 , sulphates claim 1 , halides claim 1 , acetates claim 1 , chelates claim 1 , complexes claim 1 , nanoparticles of metals from group IIA claim 1 , IIIB claim 1 , IVB claim 1 , VB claim 1 , VIB claim 1 , VIIB claim 1 , VIIIB claim 1 , IB claim 1 , IIB claim 1 , IIIA and IVA of the periodic table and mixtures thereof.3. The process according to claim 1 , wherein the catalyst is selected from the group comprising oxides claim 1 , hydroxides claim 1 , carbonates claim 1 , bicarbonates claim 1 , nitrates claim 1 , sulphates claim 1 , halides claim 1 , acetates claim 1 , chelates claim 1 , complexes claim 1 , nanoparticles of manganese claim 1 , cobalt claim 1 , nickel claim 1 , lead claim 1 , copper claim 1 , aluminium claim 1 , rhuthenium claim 1 , silver claim 1 , zinc claim 1 , cadmium claim 1 , iron claim 1 , molybdenum claim 1 , chromium claim 1 , magnesium claim 1 , vanadium claim 1 , zirconium claim 1 , indium and mixtures thereof.4. The process according to claim 1 , wherein the water used ...

Trimetallic layered double hydroxide composition

A layered double hydroxide (LDH) material, methods for using the LDH material to catalyse the oxygen evolution reaction (OER) in a water-splitting process and methods for preparing the LDH material. The LDH material includes nickel, iron and chromium species and possesses a sheet-like morphology including at least one hole.

CATALYST FOR LOW TEMPERATURE SLURRY BED FISCHER-TROPSCH SYNTHESIS

A method for controllably producing a hematite-containing Fischer-Tropsch catalyst by combining an iron nitrate solution with a precipitating agent solution at a precipitating temperature and over a precipitation time to form a precipitate comprising iron phases; holding the precipitate from at a hold temperature for a hold time to provide a hematite containing precipitate; and washing the hematite containing precipitate via contact with a wash solution and filtering, to provide a washed hematite containing catalyst. The method may further comprise promoting the washed hematite containing catalyst with a chemical promoter; spray drying the promoted hematite containing catalyst; and calcining the spray dried hematite containing catalyst to provide a calcined hematite-containing Fischer-Tropsch catalyst. 1. A method for controllably producing a hematite-containing Fischer-Tropsch catalyst , the method comprising:(a) combining an iron nitrate solution with a precipitating agent solution at a precipitating temperature and over a precipitation time to form a precipitate comprising iron phases, wherein the precipitating temperature is less than or equal to about 95° C.; wherein the iron nitrate, the precipitating agent solution, or both, comprise a refractory material;(b) holding the precipitate from (a) at a hold temperature for a hold time to provide a hematite containing precipitate; and(c) washing the hematite containing precipitate from (b) via contact with a wash solution and filtering, to provide a washed hematite containing Fischer-Tropsch catalyst.2. The method of further comprising adding a hematite promoter to control the amount of hematite in the hematite-containing Fischer-Tropsch catalyst.3. The method of wherein the hematite-containing Fischer-Tropsch catalyst comprises from about 0.5 to about 80 weight percent hematite.4. The method of wherein the hematite promoter is selected from the group consisting of basic silica claim 2 , acidic silica claim 2 , ...

METHOD FOR PREPARING REFRACTORY ALLOY-BASED POLYMETALLIC OXIDE CATALYSTS FOR THE PARTIAL OXIDATION OF HYDROCARBONS INTO SYNTHESIS GAS

The invention relates to a method for preparation of oxide-polymetallic catalysts containing platinum-group metals for steam-oxidative conversion to obtain carbon monoxide and hydrogen. The method comprises treatment of NiO and COOby solutions of Al, Ce, Zr nitrates and palladium (Pd(NH)Cl), platinum (H[PtCl]·6HO) and rhodium (H[RhCl]) compounds followed by drying, carbonization of the obtained material in a methane flow at 550° C., preparation of slurry from this material, pseudo-boehmite and tetraisopropoxysilane, filling foam nichrome pores with obtained material suspension, elimination of water at 80° C., calcinating during 3 hours in an atmosphere of argon at 1300° C., elimination of carbon by water vapors at 600° C. during 3 hours. The technical result is development of a highly efficient heterogeneous catalyst. 3 material claims, 7 tables, 4 examples. 1. The method for preparation of oxide-polymetallic catalysts containing platinum-group metals for steam-oxidative conversion of hydrocarbons to obtain carbon monoxide and hydrogen characterizes in that , it includes treatment of NiO and CoOby solutions of Al , Ce , Zr nitrates and palladium (Pd(NH)Cl) , platinum (H[PtCl]·6HO) and rhodium (H[RhCl]) compounds followed by drying , carbonization of the obtained material in a methane flow at 550° C. , preparation of slurry from this material , pseudo-boehmite and tetraisopropoxysilane , filling foam nichrome pores with obtained material suspension , elimination of water at 80° C. , calcinating during 3 hours in an atmosphere of argon at 1300° C. , elimination of carbon by water vapors at 600° C. during 3 hours.2. A method of characterized in that NiO and CoOtreatment is carried out by a solution with total concentration of 5-20%.3. A method of characterizes in that carbonization is carried out till the full reduction of NiO and CoOoxides and palladium claim 1 , platinum and rhodium compounds to the metals and accumulation of 5-10% of carbon.4. A method of ...

METHOD FOR PREPARING CATALYST USED FOR PREPARING CHLORINE, CATALYST AND METHOD FOR PREPARING CHLORINE

The present invention relates to a method for preparing catalyst used for preparing chlorine by oxidizing hydrogen chloride. The method is mixing a slurry mainly containing boron and chromium with a slurry mainly containing copper, boron, alkali-metal elements, rare-earth elements, aluminum sol, silica sol, carrier and optionally other metal elements, the mixing temperature being not more than 100° C., and the residence time being not more than 120 minutes, the mixed slurry is successively treated with spray drying, high temperature calcination, so that the catalyst is obtained. The present invention also relates to the catalyst prepared through the method, use of the catalyst used in the process of preparing chlorine by oxidizing hydrogen chloride and a method for preparing chlorine by using the catalyst. The catalyst is used for preparing chlorine by oxidizing hydrogen chloride with oxygen or air in fluidized bed reactor. 1. A method for preparing catalysts used for preparing chlorine by oxidizing hydrogen chloride , comprising the steps of:mixing a slurry A with a slurry B under the condition of a mixing temperature being >X° C. and ≦100° C., and a residence time being ≦120 minutes to obtain a mixed slurry;treating the mixed slurry with spray drying to obtain catalyst precursor particles; andcalcining the catalyst precursor particles to obtain the catalysts,wherein, X° C. is the highest value among the solidifying points of slurry A, slurry B and the mixed slurry; slurry A is acidic and contains boron and chromium; slurry B contains copper, boron, alkali-metal elements, rare-earth elements, aluminum sol, silica sol, carrier and optionally at least one of other metal elements selected from the group consisting of magnesium, calcium, barium, manganese, ruthenium and titanium.2. The method according to claim 1 , wherein slurry A is formed by mixing boron-containing compound claim 1 , chromium-containing compound and water; based on the weight of slurry A claim 1 , ...

PROCESS FOR HYDROGENOLYSIS OF GLYCEROL

A process for the hydrogenolysis of glycerol to produce propylene glycol as the major product comprising contacting the glycerol with hydrogen in the presence of a heterogeneous catalyst under conditions for the formation of propylene glycol is disclosed. In particular, propylene glycol is formed with a selectivity of greater than about 90%. 1. A process for the hydrogenolysis of glycerol to produce propylene glycol comprising:(a) contacting the glycerol with hydrogen in the presence of a heterogeneous catalyst under conditions for the formation of propylene glycol; and(b) optionally isolating the propylene glycol,wherein the heterogeneous catalyst comprises, consists essentially of or consists of Cu, Cr, Zn and Zr.2. The process of claim 1 , wherein the propylene glycol is formed as the major product in the process3. The process of claim 2 , wherein the propylene glycol is formed with a selectivity of greater than 90% claim 2 , 95% claim 2 , 96% claim 2 , 97% claim 2 , or 98%.4. The process of claim 1 , wherein the catalyst is prepared using a co-precipitation method.5. The process of claim 1 , wherein the heterogeneous catalyst comprises claim 1 , consists essentially of or consists of Cu claim 1 , Zn claim 1 , Cr and Zr in an elemental molar ratio (Cu:Zn:Cr:Zr) of 3:2:1:1 claim 1 , 3:2:1:2 claim 1 , 3:2:1:3 or 3:2:1:4.67.-. (canceled)8. The process of claim 1 , wherein the glycerol is a solution comprising at least about 50% (w/w) glycerol.9. The process of claim 8 , wherein the glycerol is an aqueous solution comprising about 60% (w/w) to about 90% (w/w) claim 8 , about 70% (w/w) to about 85% (w/w) claim 8 , about 80% (w/w) glycerol or about 70% (w/w) glycerol.10. The process of claim 1 , wherein the glycerol is crude glycerol obtained as a byproduct from the production of biodiesel.11. The process of claim 1 , wherein the conditions for the formation of propylene glycol comprise use of a catalyst loading of about 1% (w/w) to about 5% (w/w) claim 1 , about 3% (w ...

Process For Producing A Catalyst

A process for producing a catalyst having a heating element that is formed from an electrically conductive metal alloy. In the production process, the catalyst undergoes at least a first heat treatment, during which the catalyst is at least partly heated in defined fashion and cooled in a defined fashion. The steps include heating at least a subregion of the catalyst to a predeterminable temperature of at least 550 degrees celsius, holding the temperature at a constant temperature level for at least two minutes, and cooling the at least one subregion of the catalyst at a temperature transient of at least 500 Kelvin per minute.

Hydrocarbon Dehydrocyclization in the Presence of Carbon Dioxide

The invention relates to converting non-aromatic hydrocarbon in the presence of CO 2 to produce aromatic hydrocarbon. CO 2 methanation using molecular hydrogen produced during the aromatization increases aromatic hydrocarbon yield. The invention also relates to equipment and materials useful in such upgrading, to processes for carrying out such upgrading, and to the use of such processes for, e.g., natural gas upgrading.

CATALYST-CONTAINING OXYGEN TRANSPORT MEMBRANE

A method is described of producing a catalyst-containing composite oxygen ion membrane and a catalyst-containing composite oxygen ion membrane in which a porous fuel oxidation layer and a dense separation layer and optionally, a porous surface exchange layer are formed on a porous support from mixtures of (LnA)CrBOand a doped zirconia. Adding certain catalyst metals into the fuel oxidation layer not only enhances the initial oxygen flux, but also reduces the degradation rate of the oxygen flux over long-term operation. One of the possible reasons for the improved flux and stability is that the addition of the catalyst metal reduces the chemical reaction between the (LnA)CrBOand the zirconia phases during membrane fabrication and operation, as indicated by the X-ray diffraction results. 1. A method of producing an oxygen ion composite membrane comprising:{'sub': 1−x', 'x', 'w', '1−y', 'y', '3−δ, 'forming a first layer on a porous support containing a first mixture of particles of (LnA)CrBO, doped zirconia, catalyst metal M, and pore formers, where Ln is La, Y, Pr, Ce or Sm, A is Ca or Sr, B is Fe, Mn, Co, Ni, Al, Ti or combinations thereof, w is from about 0.9 to about 1.0, x is from about 0.1 to about 0.3, y is from about 0.1 to about 0.7, and δ is a value that renders the composition charge neutral, catalyst metal M is a catalyst metal or an oxide, carbonate or nitrate of a catalyst metal, wherein said catalyst metal is selected from Ru, Pd, Pt, Rh, Ni, Co, or combinations thereof{'sub': 1−x', 'x', 'w', '1−y', 'y', '3−δ', '1−x', 'x', 'w', '1−y', 'y', '3−δ, 'the first mixture containing the (LnA)CrBO, the doped zirconia and the catalyst metal M such that when sintered, the first layer will contain from about 20 vol. % to about 70 vol. % of the (LnA)CrBO, from about 30 vol. % to about 80 vol. % of the doped zirconia, and optionally from about 0.1 vol. % to about 20 vol. % of the catalyst metal M, based on the volume percentage of the total solid mass;'}{'sub': 1−x', ...

Carbon-dioxide Supplier Safe and Without Hazardous Exhaust Gas

Disclosed is a combustion chamber (10) of the carbon dioxide supplier including: a combustion chamber (10) combusting a mixture of air and fuel; an air supply unit supplying an into the combustion chamber (10); and a fuel supply unit supply in a fuel to the combustion chamber (10). Representative Figure is . 1. A carbon dioxide supplier that generates carbon dioxide by combusting fuel , comprising:{'b': '10', 'a combustion chamber () combusting a mixture of air and fuel;'}{'b': '10', 'an air supply unit supplying air into the combustion chamber (); and'}{'b': '10', 'a fuel supply unit supplying fuel to the combustion chamber (),'}{'b': '10', 'claim-text': [{'b': '11', 'a chamber member ();'}, {'b': 111', '11, 'an intake hole () provided at a first end of the chamber member () and located in an upstream of a as flow;'}, {'b': 112', '11, 'an exhaust hole () provided at a second end of the chamber member () and located in a downstream of the gas flow;'}, {'b': 113', '11', '111', '11', '111', '113', '11, 'a mixing space () where air and fuel mix, wherein the air is supplied into the chamber member () through the intake hole (), wherein the fuel is supplied into the chamber member () through the intake hole (), wherein the mixing space () is provided inside the chamber member ();'}, {'b': 12', '112', '113, 'a first catalyst () positioned between the exhaust hole () and the mixing space ();'}, {'b': 114', '112', '12, 'a combustion space () positioned between the exhaust hole () and the first catalyst ();'}, {'b': 13', '114, 'an ignition device () positioned inside the combustion space ();'}, {'b': 14', '112', '114, 'a second catalyst () positioned between the exhaust hole () and the combustion space (); and'}, {'b': 115', '112', '14, 'an exhaust space () positioned between the exhaust hole () and the second catalyst ().'}], 'wherein the combustion chamber () comprises2. The carbon dioxide supplier of claim 1 ,{'b': '12', 'wherein the first catalyst () includes an alloy ...

IRON-BASED CATALYST, METHOD FOR PREPARING THE SAME, AND METHOD FOR PRODUCING ALPHA-OLEFINS USING THE SAME

A catalyst including between 50.0 and 99.8 percent by weight of iron, between 0 and 5.0 percent by weight of a first additive, between 0 and 10 percent by weight of a second additive, and a carrier. The first additive is ruthenium, platinum, copper, cobalt, zinc, or a metal oxide thereof. The second additive is lanthanum oxide, cerium oxide, magnesium oxide, aluminum oxide, silicon dioxide, potassium oxide, manganese oxide, or zirconium oxide. 1. A catalyst , comprising , by a total weight of the catalyst:between 50.0 and 99.8 percent by weight of iron;between 0 and 5.0 percent by weight of a first additive, the first additive being ruthenium, platinum, copper, cobalt, zinc, or a metal oxide thereof;between 0 and 10 percent by weight of a second additive, the second additive being lanthanum oxide, cerium oxide, magnesium oxide, aluminum oxide, silicon dioxide, potassium oxide, manganese oxide, or zirconium oxide; anda carrier, the carrier being silicon dioxide.2. The catalyst of claim 1 , wherein a content of the first additive is between 0 and 2 wt. %; a content of the second additive is between 2 wt. % and 6 wt. %; and a content of the iron is between 60 wt. % and 97 wt. %.3. The catalyst of claim 1 , wherein a content of the carrier is between 1 wt. % and 40 wt. %; a content of the first additive is between 1 wt. % and 2 wt. %; a content of the second additive is between 2 wt. % and 6 wt. %; and the rest is the iron.4. A method for preparing the catalyst of claim 1 , the method comprising:1) mixing iron nitrate excluding crystal water, a nitrate of the first additive, and amorphous silicon dioxide with n-octanol to form a mixed solution, wherein a total weight percentage of the iron nitrate, the nitrate of the first additive, and the amorphous silicon dioxide in the mixed solution is between 3 wt. % and 20 wt. %; stirring the mixed solution so that the nitrate is dissolved and heating the mixed solution to a temperature of between 140 and 180° C.; keeping the ...

Preparation of a cobalt-containing catalyst

The present invention is directed to the preparation of a cobalt containing catalyst, a precipitate as an intermediate product, a Fischer-Tropsch catalyst and a process for producing normally gaseous, normally liquid and optionally normally solid hydrocarbons from synthesis gas. The precipitate and catalyst comprise crystalline Co(OH)(CO3)0.5, the crystals are needle shaped and have a surface area of at least 80 m2/g dry precipitate.

STAINLESS STEEL FOAM SUPPORTED CATALYSTS FOR THE OXIDATION OF AROMATIC COMPOUNDS

The invention provides a catalyst comprising iron oxide, nickel, ceria or palladium supported on stainless steel foam. The catalyst is effective in oxidising aromatic compounds such as toluene and o-cresol and, advantageously, is particularly effective when the oxidation is carried out at elevated temperatures that correspond to temperatures attained in areas of the aircraft where cabin air is recirculated. 1. A catalyst comprising iron oxide , nickel , ceria or palladium supported on stainless steel foam.2. A catalyst according to claim 1 , wherein the iron oxide claim 1 , nickel claim 1 , ceria or palladium is present in an amount of 2 to 15 wt %.3. A catalyst according to claim 1 , wherein the catalyst comprises iron oxide.4. A catalyst according to claim 1 , wherein the catalyst comprises nickel.5. A catalyst according to claim 1 , wherein the catalyst comprises ceria.6. A catalyst according to claim 1 , wherein the catalyst comprises palladium.8. A method according to claim 7 , wherein the compound in a gas containing oxygen is heated in the presence of said catalyst to a temperature of from 150° C. to 450° C. claim 7 , or 200 to 400° C.9. A method of treating air in an air handling system comprising heating the air in the presence of a catalyst comprising iron oxide claim 7 , nickel claim 7 , ceria or palladium supported on stainless steel foam.10. A method according to claim 9 , wherein the air is heated in the presence of said catalyst to a temperature of from 150° C. to 450° C. or 200 to 400° C.11. A catalyst according to claim 2 , wherein the catalyst comprises iron oxide.12. A catalyst according to claim 2 , wherein the catalyst comprises nickel.13. A catalyst according to claim 2 , wherein the catalyst comprises ceria.14. A catalyst according to claim 2 , wherein the catalyst comprises palladium. The invention relates to stainless steel foam supported catalysts which are useful in the oxidation of aromatic compounds. One aspect of the invention includes ...

Catalyst for oxidative dehydrogenation reaction, and method for producing same

Provided is a catalyst for an oxidative dehydrogenation reaction that comprises: a porous support; a core portion supported on the porous support and containing a first zinc ferrite-based catalyst; and a shell portion supported on the core portion and containing a second zinc ferrite-based catalyst, in which the first zinc ferrite-based catalyst and the second zinc ferrite-based catalyst are different from each other.

Method for producing hydride using unsaturated compound having carbon number of 4 as raw material

The present invention relates to a method for producing a hydride having a carbon number of 4, comprising contacting, in liquid phase, an unsaturated compound having a carbon number of 4 as a raw material with a solid catalyst obtained by loading a metal element belonging to Groups 9 to 11 of the long periodic table on a support, thereby performing hydrogenation to produce a corresponding hydride having a carbon number of 4, wherein hydrogenation is performed in the presence of, as a solvent, a 1,4-butanediol having a nitrogen component concentration of 1 ppm by weight to 1 wt % in terms of nitrogen atom.

Process for Preparing Fluorobenzene and Catalyst Therefore

The invention relates to process for the manufacture or preparation of fluorinated benzene, in particular monofluorobenzene, in a vapor-phase fluorination process. The process of the invention, for example, can comprise a batch or continuous manufacture or preparation of fluorinated benzene, in particular monofluorobenzene, using hydrogen fluoride (HF) in gas phase as fluorination gas. Also, in this process of the invention, for example, fluorination catalysts are involved. 1. A process for the manufacture of a fluorinated benzene , preferably monofluorobenzene , in a vapor-phase fluorination process comprising the steps of:a) provision of a chlorinated benzene as starting compound;b) provision of a fluorination gas consisting of anhydrous hydrogen fluoride (HF);c) provision of a fluorination catalyst, optionally of an activated and/or reactivated, and/or of a pre-fluorinated fluorination catalyst;d) provision of a reactor or reactor system, resistant to hydrogen fluoride (HF), and comprising a vaporizer for the starting compound of a), and a condenser for the vapor-phase fluorination reaction product, and a reservoir for collecting the fluorination reaction product;e) at least one vapor-phase reaction stage comprising reacting of a) a vaporized chlorinated benzene with b) anhydrous hydrogen fluoride (HF) in gas phase in the presence of c) the fluorination catalyst, so as to produce a vapor-phase fluorination reaction product;f) withdrawing the vapor-phase fluorination reaction product formed in the vapor-phase reaction step e) from the reactor or reactor system of d), and transferring the vapor-phase fluorination reaction product to the condenser and condensing for collecting the condensed fluorination reaction product; andg) hydrolysing the fluorination reaction product obtained and collected according to f), in water, to obtain a fluorinated benzene, preferably monofluorobenzene; andh) phase separation of the organic phase of fluorinated benzene, preferably ...

ALKANE ACTIVATION WITH SINGLE AND BI-METALLIC CATALYSTS

Methods, compositions, and articles of manufacture for alkane activation with single- or bi-metallic catalysts on crystalline mixed oxide supports. 1. A catalytic article of manufacture comprising:{'sub': x', '1-x', 'y', '1-y', '3, 'a support comprising either a perovskite having the composition LaSrCrFeOwhere x is greater than 0 and less than 1, y is 0.3 to 0.7; and'}a metallic catalyst selected from the group consisting of metallic and bi-metallic catalysts.2. The catalytic article of manufacture of claim 1 , wherein the support comprises a perovskite and wherein x is 0.3 to 0.7.3. The catalytic article of manufacture of claim 1 , wherein the support comprises a perovskite and wherein x is 0.75 and y is 0.7.4. The catalytic article of manufacture of claim 1 , wherein the support comprises a perovskite and wherein y is 0.5.5. The catalytic article of manufacture of claim 2 , wherein metallic catalyst is a single metal catalyst.6. The catalytic article of manufacture of claim 3 , wherein the single metal catalyst is selected from the group consisting of Mo claim 3 , Co claim 3 , and Ce.7. The catalytic article of manufacture of claim 1 , wherein the metallic catalyst is Ce and further wherein the metallic catalyst is doped within the perovskite of the support.8. The catalytic article of manufacture of claim 1 , wherein the support comprises a fluorite and wherein z is 0.1.9. The catalytic article of manufacture of wherein the metallic catalyst is a bimetallic catalyst.10. The catalytic article of manufacture of claim 9 , wherein the bimetallic catalyst comprises Pt as a first metal.11. The catalytic article of manufacture of claim 10 , wherein a second metal of the bimetallic catalyst is selected from the group comprising Re claim 10 , Co claim 10 , and Ga.12. A catalytic article of manufacture comprising:{'sub': '2', 'a support comprising amorphous SiO; and'}a bi-metallic catalyst deposited on the support.13. The catalytic article of manufacture of claim 12 , ...

CATALYST FOR FIXED BED ANILINE RECTIFICATION RESIDUE RECYCLING AND PREPARATION METHOD

The present invention relates to a catalyst for fixed bed aniline rectification residue recycling and preparation method thereof. Based on the total weight of the catalyst, the catalyst comprises the following components in percentage by weight: 5-40% of an active component, 2-30% of a first cocatalyst component, 10-30% of a second cocatalyst component and the balance of carrier, wherein the active component is NiO; the first cocatalyst component is one or more of Fe, Mo, Cr or Co oxide; and the second cocatalyst component is one or more of La, Zr, Y or Ce oxide. The catalyst is prepared through co-precipitation. The catalyst shows high activity and stability in the waste liquid treatment process, and can still maintain high rectification residue cracking rate after reaction of 200 hours. 1. A process of recycling aniline rectification residue , comprising subjecting the aniline rectification residue to fixed bed hydrogenation with a catalyst , wherein said catalyst comprises the components described below based on the total weight of the catalyst:5-40 wt % of NiO as an active component,2-30 wt % of one or more selected from oxides of Fe, oxides of Mo, oxides of Cr and oxides of Co as a first cocatalyst component,10-30 wt % of one or more selected from oxides of La, oxides of Zr, oxides of Y and oxides of Ce as a second cocatalyst component,the remaining portion being the support.2. The process of claim 1 , wherein said catalyst comprises the components described below based on the total weight of the catalyst:15-30 wt % of NiO as the active component,5-25 wt % of one or more selected from oxides of Fe, oxides of Mo, oxides of Cr and oxides of Co as the first cocatalyst component,15-25 wt % of one or more selected from oxides of La, oxides of Zr, oxides of Y and oxides of Ce as the second cocatalyst component,the remaining portion being the support.3. The process of claim 1 , wherein the support is SiO.4. The process of claim 1 , wherein the aniline rectification ...

Hydrocarbon Dehydrocyclization in the Presence of Carbon Dioxide

The invention relates to converting non-aromatic hydrocarbon in the presence of COto produce aromatic hydrocarbon. COmethanation using molecular hydrogen produced during the aromatization increases aromatic hydrocarbon yield. The invention also relates to equipment and materials useful in such upgrading, to processes for carrying out such upgrading, and to the use of such processes for, e.g., natural gas upgrading. 1. A hydrocarbon conversion process , comprising:{'sub': 2+', '2, '(a) providing a feed comprising ≧1 wt. % of C non-aromatic hydrocarbon and ≧0.1 wt. % of CO;'} the first catalyst includes (i) ≧0.005 wt. % of a dehydrogenation component which comprises one or more of Ga, Zn, Mo, W, La, Pt, and Pd, and (ii) ≧10 wt. % of a molecular sieve component, the molecular sieve component comprising at least one molecular sieve having a Constraint Index in the range of from 1 to 12, and', {'sub': '2', 'the second catalyst includes ≧0.005 wt. % of a COconversion component which comprises one or more of Ru, Rh, Ni, Co, and Fe;'}], '(b) providing first and second catalysts, wherein'}{'sub': 2+', '2, "(c) exposing the feed to the first catalyst under conversion conditions effective for (i) converting ≧10 wt. % of the feed's C non-aromatic hydrocarbon to aromatic hydrocarbon and molecular hydrogen and (ii) increasing aromatic hydrocarbon yield by reacting ≧1 wt. % of the feed's COwith at least a portion of the molecular hydrogen in the presence of the second catalyst to produce methane and water."}2. The process of claim 1 , wherein the feed comprises ≧1 wt. % of CO; 10 wt. % to 40 wt. % ethane; 20 wt. % to 50 wt. % propane claim 1 , and 20 wt. % to 50 wt. % butanes claim 1 , and further comprises 1 wt. % to 40 wt. % methane and ≦1 wt. % of aromatic hydrocarbon.3. The process of claim 1 , wherein the COreaction of step (c) has a greater selectivity for methane than CO.4. The process of claim 1 , wherein (i) the first catalyst includes (i) ≧0.01 wt. % of the ...

PEROVSKITE CATALYSTS ENHANCED COMBUSTION ON POROUS MEDIA

The effects of different perovskite catalysts, catalytic active materials with a crystal structure of ABO, on matrix stabilized combustion in a porous ceramic media are explored. Highly porous silicon carbide ceramics are used as a porous media for a catalytically enhanced matrix stabilized combustion of a lean mixture of methane and air. A stainless steel combustion chamber was designed incorporating a window for direct observation of the flame within the porous media. Perovskite catalytic enhancement of SiC porous matrix with La0.75Sr0.25Fe0.6Cr0.35Ru0.05O3; La0.75Sr0.25Fe0.6Cr0.4O3; La0.75Sr0.25Fe0.95Ru0.05O3; La0.75Sr0.25Cr0.95Ru0.05O3; and LaFe0.95Ru0.05O3, for example, were used to enhance combustion. The flammability limits of the combustion of methane and air were explored using both inert and catalytically enhanced surfaces of the porous ceramic media. By coating the SiC porous media with perovskite catalysts it was possible to lower the minimum stable equivalence ratio. 1. A matrix stabilized porous burner comprising:{'sub': 0.75', '0.25', '0.6', '0.35', '0.05', '3', '0.75', '0.25', '0.6', '0.4', '3', '0.75', '0.25', '0.95', '0.05', '3', '0.75', '0.05', '0.95', '0.05', '3', '0.95', '0.05', '3, 'a combustion chamber comprising a porous ceramic matrix catalytically enhanced with a perovskite catalyst composition selected from the group consisting of LaSrFeCrRuO; LaSrFeCrO; LaSrFeRuO; LaSrCrRuO; and LaFeRuO.'}2. The burner of claim 1 , wherein the porous ceramic matrix comprises a silicon carbide porous ceramic matrix portion claim 1 , and the perovskite catalyst is coated on the surface of the porous silicon carbide ceramic matrix portion.3. The burner of claim 2 , wherein the porous ceramic matrix further comprises an alumina porous ceramic matrix portion positioned adjacent to the silicon carbide porous ceramic matrix portion.4. The burner of claim 1 , wherein the burner produces a stabilized combustion of a lean mixture of natural gas and air.5. The ...

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

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

Catalytic funneling of phenolics

In general, present invention concerns an integrated wood-to-xylochemicals biorefinery, enabling production of renewable phenol, phenolic oligomers, propylene, and carbohydrate pulp from lignocellulosic biomass.

ALKANE ACTIVATION WITH SINGLE AND BI-METALLIC CATALYSTS

Methods, compositions, and articles of manufacture for alkane activation with single- or bi-metallic catalysts on crystalline mixed oxide supports. 1. A catalytic article of manufacture comprising:{'sub': '2', 'a support comprising amorphous SiO; and'}a bi-metallic catalyst deposited on the support.2. The catalytic article of manufacture of claim 1 , wherein the bimetallic catalyst comprises Pt as a first metal.3. The catalytic article of manufacture of claim 1 , wherein a second metal of the bimetallic catalyst comprises Co.4. The catalytic article of manufacture of claim 1 , wherein a second metal of the bimetallic catalyst comprises Mo.5. A method for non-oxidative coupling of methane comprising:{'sub': '2', 'synthesizing a bi-metallic on a SiOsupport to form a bimetallic catalyst;'}converting methane to ethylene with an initial conversion of 8%.6. The method of claim 5 , wherein the bimetallic catalyst has an initial selectivity in the conversion of methane to ethylene of at least 80%.7. The method of claim 5 , wherein the conversion of methane is at a temperature of between 550° C. and 650° C.8. The method of claim 5 , wherein synthesizing comprises a sequential grafting of Co onto the SiOsupport claim 5 , forming SiOsupported Co.9. The method of claim 8 , wherein the synthesizing further comprises calcinating the SiOsupported Co is impregnated with Pt and reduced.10. The method of claim 9 , wherein the sequential grafting method comprises strong electrostatic adsorption.11. The method of claim 4 , wherein synthesizing comprises a sequential grafting of Mo onto the SiOsupport forming SiOsupported Mo.12. The method of claim 11 , wherein the sequential grafting method comprises incipient wetness impregnation.13. The method of claim 12 , wherein the synthesizing further comprises calcinating the SiOsupported Mo is impregnated with Pt and reduced. This application is a divisional and claims the benefit of and priority to U.S. patent application Ser. No. 15/691,666, ...

PREPARATION METHOD OF PARTICLE SIZE-CONTROLLED, CHROMIUM OXIDE PARTICLES OR COMPOSITE PARTICLES OF IRON OXIDE-CHROMIUM ALLOY AND CHROMIUM OXIDE

Provided are particle size-controlled, chromium oxide particles or composite particles of iron oxide-chromium alloy and chromium oxide; a preparation method thereof; and use thereof, in which the chromium oxide particles or the composite particles of iron oxide-chromium alloy and chromium oxide having a desired particle size are prepared in a simpler and more efficient manner by using porous carbon material particles having a large pore volume as a sacrificial template. When the chromium oxide particles or the composite particles of iron oxide-chromium alloy and chromium oxide thus obtained are applied to gas-phase and liquid-phase catalytic reactions, they are advantageous in terms of diffusion of reactants due to particle uniformity, high-temperature stability may be obtained, and excellent reaction results may be obtained under severe reaction environment. 1. A method of preparing particle size-controlled chromium oxide particles , the method comprising:{'sup': '3', 'Step 1a of preparing porous carbon material particles having a pore volume of 0.3 cm/g or more;'}Step 2a of mixing a chromium hydrate salt and the porous carbon material particles;Step 3a of melt-infiltrating the chromium hydrate salt into pores of the porous carbon material particles at a temperature, at which the chromium hydrate salt is melted; andStep 4a of calcining the chromium hydrate salt and the porous carbon material at a high temperature of 700 to 900° C. to form chromium oxide particles, of which particle size is controlled by the pores of the porous carbon material, and also removing the porous carbon material by pyrolysis to remain particle size-controlled chromium oxide particles.2. The method of claim 1 , wherein coefficient of variation (CV) of the particle size of the chromium oxide particles is 0.3 or less.3. The method of claim 1 , wherein an average pore size of the porous carbon material particle in Step 1a is 2 nm to 50 nm.4. The method of claim 1 , wherein an average particle ...

Chromium- and nickel-free hydrogenation of hydroformylation mixtures

The invention is concerned with catalysts for heterogeneous hydrogenation of oxo process aldehydes. The problem addressed by the invention is that of developing a catalyst containing neither chromium nor nickel. In addition, it is to enable the economically viable hydrogenation of aldehyde mixtures originating from industrial oxo processes on the industrial scale. For this purpose, the catalyst should not be reliant on costly precious metals such as Ru, Pd or Pt. This problem was solved by omitting the chromium and nickel in the preparation of a conventional Cu/Ni/Cr system, such that a catalyst wherein only copper occurs as hydrogenation-active component on the support material thereof, and not chromium or nickel, is obtained. What is surprising here is that a functioning catalyst for the purpose intended still arises at all even though two of three hydrogenation-active metals are omitted. However, this requires as necessary conditions that support material used is silicon dioxide and that the content of Cu and SiO 2 in the active catalyst is set accurately within very tight limits.

PROCESS FOR THE MANUFACTURE OF 2-CHLORO-3,3,3-TRIFLUOROPROPENE BY GAS PHASE FLUORINATION OF PENTACHLOROPROPANE

The present invention provides a process of catalytic fluorination in gas phase of product 1,1,1,2,3-pentachloropropane or/and 1,1,2,2,3-pentachloropropane into product 2-chloro-3,3,3-trifluoropropene in presence of a catalyst and oxygen. 1. Process of catalytic fluorination in gas phase of product 1 ,1 ,1 ,2 ,3-pentachloropropane and/or 1 ,1 ,2 ,2 ,3-pentachloropropane into product 2-chloro-3 ,3 ,3-trifluoropropene in presence of a catalyst and oxygen.2. Process according to claim 1 , wherein the ratio of oxygen with respect to pentachloropropane (240) is 0.05 to 15 mole % claim 1 , preferably 0.5 to 10 mole %.3. Process according to any one of to claim 1 , carried out in the presence of a catalyst comprising Ni—Cr claim 1 , preferably supported.4. Process according to any one of to claim 1 , wherein said catalyst is supported on a support selected from fluorinated alumina claim 1 , fluorinated chromia claim 1 , fluorinated activated carbon or graphite carbon.5. Process according to any one of to claim 1 , wherein said catalyst further comprises a co-catalyst selected from Ni claim 1 , Co claim 1 , Zn claim 1 , Mn or mixtures thereof claim 1 , preferably nickel claim 1 , and wherein said co-catalyst is preferably present in an amount from about 1-10 wt % of said fluorination catalyst.6. Process according to any one of to claim 1 , wherein said fluorination catalyst is activated with a fluorine-containing compound claim 1 , preferably hydrogen fluoride claim 1 , and preferably at a pressure above 10 bars.7. Process according to one of the to claim 1 , in which the 1 claim 1 ,1 claim 1 ,1 claim 1 ,2 claim 1 ,3-pentachloropropane contains up to 40 mol % of isomer 1 claim 1 ,1 claim 1 ,2 claim 1 ,2 claim 1 ,3-pentachloropropane.8. Process according to any one of to claim 1 , which is carried out at a pressure from 1 to 20 bars claim 1 , preferably 3 to 15 bars claim 1 , more preferably 5 to 10 bars.9. Process according to any one of to claim 1 , carried out at a ...

Cu-based catalyst, its preparation process and use thereof

The present invention relates to a Cu-based catalyst, a preparation process thereof and its use as the dehydrogenation catalyst in producing a hydroxyketone compound such as acetoin. Said Cu-based catalyst contains copper, at least one auxiliary metal selected from metal of Group IIA, non-noble metal of Group VIII, metal of Group VIB, metal of Group VIIB, metal of Group IIB and lanthanide metal of periodic table of elements, and an alkali metal, and further contains at least one ketone additive selected from a ketone represented by formula (II) and a ketone represented by formula (II′). Said Cu-based catalyst shows a high the acetoin selectivity as the dehydrogenation catalyst for producing acetoin. 1. A Cu-based catalyst , which contains Cu , at least one auxiliary metal selected from metal of Group IIA (preferably at least one of Mg and Ca) , non-noble metal of Group VIII (preferably at least one of Fe and Ni) , metal of Group VIB (preferably Cr) , metal of Group VIIB (preferably Mn) , metal of Group IIB (preferably Zn) and lanthanide metal (preferably ytterbium) of periodic table of elements , an alkali metal and optionally a binder (preferably at least one inorganic binder selected from refractory oxide and aluminosilicate , more preferably at least one inorganic binder selected from alumina , bauxite , pseudo-boehmite , silica , silica-alumina , boehmite , attapulgite , bentonite , kaolin , diatomite and montmorillonite , more preferably at least one inorganic binder selected from alumina , silica , diatomite and kaolin , more preferably alumina) , and further contains at least one ketone additive selected from a ketone represented by formula (II) and a ketone represented by formula (II′) (preferably acetoin) , and optionally a solvent (preferably at least one of C1-6 alcohols , more preferably at least one of C1-6 linear or branched monohydric alcohols , more preferably at least one of methanol and ethanol) ,{'br': None, 'R1-C(═O)—CH(OH)—R2\u2003\u2003(II)'}{' ...

Butadiene preparation method providing excellent catalyst reproducibility

A method of preparing butadiene that includes supplying butene, oxygen, nitrogen, and steam into a reactor filled with a metal oxide catalyst, and performing an oxidative dehydrogenation reaction at a temperature of 300 to 450° C. as a reaction step; after the reaction step, maintaining supplying the butene, oxygen, nitrogen, and steam within a range within which the flow rate change of the butene, oxygen, nitrogen, and steam is less than ±40%, or stopping supplying the butene, and cooling the reactor to a temperature range of 200° C. or lower and higher than 70° C. as a first cooling step; and after the first cooling step, stopping supplying the butene, oxygen, nitrogen, and steam or stopping at least supplying the butene, and cooling the reactor to a temperature of 70° C. or lower as a second cooling step.

HEAT INTEGRATED REFORMER WITH CATALYTIC COMBUSTION FOR HYDROGEN PRODUCTION

An apparatus for the production of hydrogen from a fuel source includes a combustor configured to receive a combustor fuel and convert the combustor fuel into a combustor heat; a reformer disposed annularly about the combustor, a removable structured catalyst support disposed within the gap and coated with a catalyst to induce combustor fuel combustion reactions that convert the combustor fuel to the combustor heat, and a combustor fuel injection aperture configured for mixing combustion fuel into the combustion catalyst. The combustor fuel injection aperture being disposed along a length of the combustion zone. The reformer and the combustor define a gap therebetween and the reformer is configured to receive the combustor heat. 1. An apparatus for the production of hydrogen from a fuel source , comprising:a combustor configured to receive a combustor fuel and convert the combustor fuel into combustor heat;a reformer disposed annularly about the combustor, wherein the reformer and the combustor define a gap therebetween and the reformer is configured to receive the combustor heat;a removable structured catalyst support disposed within the gap and coated with a catalyst to induce combustor fuel combustion reactions that convert the combustor fuel to the combustor heat, the structured catalyst support being in contact with the combustor and the reformer, forming heat exchange zones where heat is transferred between a feed of the combustor and products of the reformer, and between a feed of the reformer and products of the combustor; anda combustor fuel injection aperture configured for mixing combustion fuel into the combustion catalyst, the combustor fuel injection aperture being disposed along a length of the combustion zone.2. The apparatus of claim 1 , wherein the combustor fuel injection aperture includes an annular ring including injector holes along a perimeter of the annular ring.3. The apparatus of claim 2 , wherein the reformer is configured to receive at ...

Mixed Metal Oxide Catalysts and Methods for Olefin Production in an Oxidative Dehydrogenation Reaction Process

A catalyst structure includes a plurality of metal oxides formed on a support, where the support includes zirconia and/or silica. The metal oxides include at least three metals selected from the group consisting of chromium, iron, nickel, and a platinum group metal. The catalyst structure can be used in an oxidative dehydrogenation (ODH) reaction process for converting an alkane to an olefin. In some embodiments, carbon dioxide utilized in the ODH reaction process is obtained from a flue gas derived from a fossil fuel burning power plant. 1. A catalyst structure comprising a plurality of metal oxides formed on a support comprising zirconia and/or silica , the metal oxides comprising at least three metals selected from the group consisting of chromium , iron , nickel , and a platinum group metal.2. The catalyst structure of claim 1 , wherein the platinum group metal is selected from the group consisting of platinum claim 1 , palladium claim 1 , ruthenium and rhodium.3. The catalyst structure of claim 1 , wherein the metal oxides comprise nickel oxide present in an amount from about 0.01% to about 10% by weight of the catalyst structure.4. The catalyst structure of claim 3 , wherein the nickel oxide is present in an amount of no greater than about 1% by weight of the catalyst structure.5. The catalyst structure of claim 1 , wherein the metal oxides comprise chromium oxide in an amount from about 0.01% to about 30% by weight of the catalyst structure.6. The catalyst structure of claim 1 , wherein the metal oxides comprise iron oxide in an amount from about 0.01% to about 30% by weight of the catalyst structure.7. The catalyst structure of claim 1 , wherein the metal oxides comprise chromium oxide in an amount of at least about 5% by weight of the catalyst structure claim 1 , iron oxide in an amount of at least about 5% by weight of the catalyst structure claim 1 , and nickel oxide in an amount of no greater than about 1% by weight of the catalyst structure.8. The ...

CATALYSTS FOR PREPARATION OF BUTADIENE BY OXYDEHYDROGENATION OF BUTENE IN FLUIDIZED BED REACTOR AND METHOD OF PREPARING SAME AND USE OF SAME

The invention relates to a catalyst for preparation of butadiene by oxydehydrogenation of butene in a fluidized bed reactor, a method of preparing the same, and use of the same, wherein a method according to an embodiment of the invention comprises: reacting a metal precursor with an alkaline substance to obtain a slurry containing insoluble compound, followed by filtering and washing the slurry; adding a binder and deionized water, followed by agitation to regulate the solid content of the slurry to 10-50%; subjecting the slurry to spray drying granulation, wherein the temperature at the feed port is controlled between 200-400° C., and the temperature at the discharge port is controlled between 100-160° C., to obtain catalyst microspheres; and drying the catalyst microspheres at 80-200° C. for 1-24 h, and then calcining the catalyst microspheres at 500-900° C. for 4-24 h to obtain a catalyst having a general formula of FeXaYbZcOd, comprising Fe, Mg, Zn, Bi, Mo, Mn, Ni, Co, Ba, Ca, and other metals. The catalyst microspheres prepared according to the exemplary method exhibit high mobility, desirable particle size distribution, extremely high mechanical strength and catalytic activity, and are applicable to industrial production of butadiene by oxydehydrogenation of butene in a fluidized bed. When this catalyst is used to prepare butadiene by oxydehydrogenation of butene, the yield of butadiene is 76-86%, and the selectivity to butadiene is 94-97%. 1. A method of preparing a catalyst for preparation of butadiene by oxydehydrogenation of butene in a fluidized bed reactor , said method comprising the steps of:(1) reacting a metal precursor with an alkaline substance to obtain a slurry containing an insoluble compound, followed by filtering and washing the slurry;(2) adding an appropriate amount of a binder and deionized water, followed by agitating to regulate the solid content of the slurry to 10-50%, wherein the percentage is calculated by mass;(3) subjecting the ...

Catalyst for polyol hydrogenolysis

Ethylene glycol and propylene glycol may be made by hydrogenolysis of a polyol comprising the steps of reacting a polyol with hydrogen in the presence of a hydrogenolysis catalyst. The hydrogenolysis comprises nickel, one or more promoter, and one or more support. The promoter is selected from bismuth, silver, tin, antimony, gold, lead, thallium, cerium, lanthanum, and manganese. The support is selected from zirconia and carbon. A zirconia support comprises a zirconia textual promoter, which is selected from Cr, Mo, W, Nb, Ce, Ca, Mg, La, Pr, Nd, Al, and P. If the support comprises carbon, then the promoter is selected from bismuth and antimony. In another embodiment, if the support comprises carbon, then both the promoter is selected from bismuth and antimony, and the catalyst comprises copper. In another embodiment, the catalyst additionally comprises copper.

EXHAUST PURIFYING APPARATUS

An exhaust purifying apparatus is provided, that can be manufactured at low manufacturing costs and is capable exhibiting high exhaust purifying performance. The exhaust purifying apparatus includes an exhaust passage, and an exhaust purifying member disposed in the exhaust passage. The exhaust purifying member is made of stainless steel. The surface of the stainless steel material is not covered with a catalyst coat containing a catalyst component, so that the surface of the stainless steel material is brought into contact with exhaust. The exhaust purifying member is made of precipitation hardening stainless steel and/or austenitic stainless steel. 1. An exhaust purifying apparatus comprising:{'b': '1', 'an exhaust passage ();'}{'b': 2', '1', '2, 'an exhaust purifying member () disposed in the exhaust passage (), wherein the exhaust purifying member () is made of stainless steel, and'}{'b': '25', 'a surface of the stainless steel material is not covered with a catalyst coat containing a catalyst component, so that the surface of the stainless steel material is brought into contact with exhaust ().'}22. The exhaust purifying apparatus according to claim 1 , wherein the exhaust purifying member () is made of precipitation hardening stainless steel and/or austenitic stainless steel.32222122228abcabc. The exhaust purifying apparatus according to claim 1 , wherein the exhaust purifying member () includes a plurality of plate members () () () made of stainless steel and keeping a predetermined interval in a passage forming direction of the exhaust passage () claim 1 , and the plate members () () () each include an exhaust passing hole ().422ab. The exhaust purifying apparatus according to claim 3 , wherein the plate member () on a most exhaust upstream side is formed to be greater in thickness than a predetermined one of the plate members () on an exhaust downstream side.522cb. The exhaust purifying apparatus according to claim 3 , wherein the plate member () on a most ...

METHOD FOR THE SELECTIVE PRODUCTION OF N-METHYL-PARA-ANISIDINE

The invention “Method for selective synthesis of N-methyl-para-anisidine” relates to chemical technology processes, namely to catalytic alkylation of aromatic amines and nitro compounds. 1. The process for synthesis of N-methyl-para-anisidine , consist in that N-alkylation of para-nitroanisole and/or para-anisidine is performed in vapor phase on dehydrogenating catalyst at a temperature 180-260° C. and atmospheric pressure with subsequent product isolation using rectification.2. The process of wherein N-methyl-para-anisidine is produced claim 1 , correspondingly claim 1 , from para-nitroanisole.3. The process of wherein N-methyl-para-anisidine is produced claim 1 , correspondingly claim 1 , from para-anisidine.4. The process of wherein N-alkylation is performed in nitrogen stream.5. The process of wherein N-alkylation is performed in hydrogen stream.6. The process of wherein the catalyst has the following composition: CuO—55%; ZnO—10.5%; CrO—13.5%; AlO0 the rest.7. The process of wherein the catalyst has the following composition CuO—25%; ZnO—25%; CaO—5%; AlO—the rest.8. The process of wherein the catalyst has the following composition: CuO—25-45%; BaO—2-10%; TiO—15-35%; CrO—the rest.9. The process of wherein the catalyst has the following composition: CuO—35-45%; ZnO—25-35%; NiO—3-8%; AlO—the rest.10. The process of wherein the catalyst has the following composition: CuO—12-19% MnO—2-3%; CrO—1.0-1.4%; FeO—1.0-1.4%; CoO—0.5-0.8%; AlO—the rest.11. The process of wherein Raney nickel catalyst is used.12. The process of wherein BASF Cu-E403TR catalyst is used with the following composition: copper chromite—67-71% claim 6 , copper—11-15% claim 6 , copper oxide—8-21% claim 6 , graphite—0-4% claim 6 , chromium (3+) oxide—0-3%.13. The process of wherein BASF Cu-0203T 1/8 catalyst is used with the following composition: copper oxide—75-100% claim 6 , chromium (3+) oxide—0.1-1%.14. The process of wherein BASF Cu-E406 TR catalyst is used with the following composition: Cu—36% ...

CATALYTIC GAS PHASE FLUORINATION

The invention relates to a fluorination process, alternately comprising reaction stages and regeneration stages, wherein the reaction stages comprise reacting a chlorinated compound with hydrogen fluoride in gas phase in the presence of a fluorination catalyst to produce a fluorinated compound, and the regeneration stages comprise contacting the fluorination catalyst with an oxidizing agent-containing gas flow. 1. A fluorination process , alternately comprising reaction stages and regeneration stages , wherein the reaction stages comprise reacting a chlorinated compound with hydrogen fluoride in gas phase in the presence of a fluorination catalyst to produce a fluorinated compound , and the regeneration stages comprise contacting the fluorination catalyst with an oxidizing agent-containing gas flow.2. The fluorination process of claim 1 , comprising a preliminary activation stage which comprises contacting the fluorination catalyst with an oxidizing agent-containing gas flow.3. The process of or claim 1 , wherein the oxidizing agent-containing gas flow of the activation stage and/or the regeneration stages is an oxygen-containing gas flow.4. The process of one of to claim 1 , wherein the activation stage and/or the regeneration stages comprise contacting the fluorination catalyst with the oxidizing agent-containing gas flow for at least 2 hours claim 1 , preferably for at least 4 hours claim 1 , more preferably for at least 10 hours claim 1 , and even more preferably for at least 15 hours.5. The process of one of to claim 1 , wherein the oxidizing agent-containing gas flow of the activation stage and/or the regeneration stages contains hydrogen fluoride in addition to the oxidizing agent claim 1 , and wherein the proportion of oxidizing agent in the oxidizing agent-containing gas flow of the activation stage and/or the regeneration stages is preferably from 2 to 98 mol % claim 1 , and more preferably from 5 to 50 mol % claim 1 , relative to the total amount ...

CATALYTIC GAS PHASE FLUORINATION

The present invention relates to a fluorination process, comprising: 1. A fluorination process , comprising:an activation stage comprising contacting a fluorination catalyst with an oxidizing agent-containing gas flow for at least one hour; andat least one reaction stage comprising reacting a chlorinated compound with hydrogen fluoride in gas phase in the presence of the fluorination catalyst, so as to produce a fluorinated compound.2. The process of claim 1 , comprising a plurality of reaction stages alternating with a plurality of regeneration stages claim 1 , wherein the reaction stages comprise reacting the chlorinated compound with hydrogen fluoride in gas phase in the presence of the fluorination catalyst claim 1 , and the regeneration stages comprise contacting the fluorination catalyst with an oxidizing agent-containing gas flow.3. The process of or claim 1 , wherein the oxidizing agent-containing gas flow of the activation stage and/or the regeneration stages is an oxygen-containing gas flow.4. The process of one of to claim 1 , wherein the activation stage and/or the regeneration stages comprise contacting the fluorination catalyst with the oxidizing agent-containing gas flow for at least 2 hours claim 1 , preferably for at least 4 hours claim 1 , more preferably for at least 10 hours claim 1 , and even more preferably for at least 15 hours.5. The process of one of to claim 1 , wherein the oxidizing agent-containing gas flow of the activation stage and/or the regeneration stages contains hydrogen fluoride in addition to the oxidizing agent claim 1 , and wherein the proportion of oxidizing agent in the oxidizing agent-containing gas flow of the activation stage and/or the regeneration stages is preferably from 2 to 98 mol % claim 1 , and more preferably from 5 to 50 mol % claim 1 , relative to the total amount oxidizing agent and hydrogen fluoride.6. The process of one of to claim 1 , wherein the oxidizing agent-containing gas flow of the activation stage ...

PROCESS FOR THE MANUFACTURE OF 2,3,3,3-TETRAFLUOROPROPENE BY GAS PHASE FLUORINATION OF PENTACHLOROPROPANE

The present invention provides a process of catalytic fluorination in gas phase of product 1,1,1,2,3-pentachloropropane or/and 1,1,2,2,3-pentachloropropane into product 2,3,3,3-tetrafluoropropene in presence of a catalyst. 1. Process of catalytic fluorination in gas phase of product 1 ,1 ,1 ,2 ,3-pentachloropropane and/or 1 ,1 ,2 ,2 ,3-pentachloropropane into product 2 ,3 ,3 ,3-tetrafluoropropene.2. Process according to claim 1 , carried out in a single stage claim 1 , preferably in one reactor claim 1 , more preferably in one catalytic bed.3. Process according to or claim 1 , wherein the product 2 claim 1 ,3 claim 1 ,3 claim 1 ,3-tetrafluoropropene is present at a concentration of at least 1% claim 1 , preferably more than 2% claim 1 , more preferably more than 3%.4. Process according to any one of to claim 1 , wherein said catalyst is a chromium catalyst claim 1 , supported or unsupported claim 1 , preferably unsupported.5. Process according to any one of to claim 1 , wherein said catalyst further comprises a co-catalyst selected from Ni claim 1 , Co claim 1 , Zn claim 1 , Mn claim 1 , Mg or mixtures thereof claim 1 , preferably nickel or magnesium claim 1 , and wherein said co-catalyst is preferably present in an amount from about 1-10 wt % of said fluorination catalyst.6. Process according to any one of to claim 1 , carried out in the presence of a catalyst comprising Ni—Cr claim 1 , preferably supported.7. Process according to any one of to claim 1 , wherein said catalyst is supported on a support selected from fluorinated alumina claim 1 , fluorinated chromia claim 1 , fluorinated activated ca bon or graphite carbon.8. Process according to any one of to claim 1 , wherein said fluorination catalyst is activated with a fluorine-containing compound claim 1 , preferably hydrogen fluoride.9. Process according to one of the to claim 1 , in which the 1 claim 1 ,1 claim 1 ,1 claim 1 ,2 claim 1 ,3-pentachloropropane contains up to 40 mole of isomer 1 claim 1 ,1 claim 1 ...

CATALYST COMPOSITION FOR CONVERSION OF SULFUR TRIOXIDE AND HYDROGEN PRODUCTION PROCESS

The present disclosure relates to a catalyst composition for conversion of sulphur trioxide to sulphur dioxide and oxygen comprising an active material selected from the group consisting of transitional metal oxide, mixed transitional metal oxide, and combinations thereof; and a support material selected from the group consisting of silica, titania, zirconia, carbides, and combinations thereof. The subject matter also relates to a process for the preparation of the catalyst composition for conversion of sulphur trioxide to sulphur dioxide and oxygen. 1. A catalyst composition for conversion of sulphur trioxide to sulphur dioxide and oxygen comprising:an active material selected from the group consisting of transitional metal oxide, mixed transitional metal oxide, and combinations thereof; anda support material selected from the group consisting of silica, titania, zirconia, carbides, and combinations thereof, wherein the active material to the support material weight ratio is in the range of 0.1 to 25 wt %.2. The catalyst composition as claimed in claim 1 , wherein the transitional metal is selected from the group consisting of Cu claim 1 , Cr claim 1 , and Fe.3. The catalyst composition as claimed in claim 1 , wherein the active material is transitional metal oxide selected from the group consisting oxides of Cu claim 1 , Cr claim 1 , and Fe.4. The catalyst composition as claimed in claim 1 , wherein the active material is mixed transitional metal oxide selected from the group consisting of binary oxide claim 1 , a ternary oxide claim 1 , and a spinel.5. The catalyst composition as claimed in claim 1 , wherein the active material is an oxide of Cu.6. The catalyst composition as claimed in claim 1 , wherein the active material is an oxide of Cr.7. The catalyst composition as claimed in claim 1 , wherein the active material is an oxide of Fe.8. The catalyst composition as claimed in claim 1 , wherein the active material is a binary oxide of Cu claim 1 , and Fe in the ...

PROCESS FOR CONVERSION OF SULFUR TRIOXIDE AND HYDROGEN PRODUCTION

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

METHOD FOR FORMING METAL OXIDE COATING LAYER ON CATALYST SUBSTRATE, CATALYST SUBSTRATE INCLUDING METAL OXIDE COATING LAYER AND CATALYST APPARATUS

An embodiment of the present invention provides a method for forming a metal oxide coating layer on a catalyst support, which comprises a precipitation step for forming a metal-containing precipitate on the catalyst support by contacting the catalyst support with a mixed solution containing a metal oxide precursor and a precipitant, and a calcination step for calcinating the metal-containing precipitate produced on the catalyst support to produce the metal oxide coating layer on the catalyst support. 1. A method for forming a metal oxide coating layer on a catalyst support , the method comprising the steps of:precipitation for forming a metal-containing precipitate on the catalyst support by contacting the catalyst support with a mixed solution containing a metal oxide precursor and a precipitant; andcalcination for calcinating the metal-containing precipitate formed on the catalyst support to form the metal oxide coating layer on the catalyst support.2. The method of claim 1 , wherein the metal oxide coating layer is an alumina coating layer and the metal is aluminum.3. The method of claim 1 , wherein the metal-containing precipitate is boehmite (AlO(OH)) or bayerite (Al(OH)).4. The method of claim 1 , wherein the metal oxide coating layer is formed in a structure in which a plurality of round or needle-shaped particles is closely packed.5. The method of claim 1 , wherein the metal oxide precursor is one or more kinds selected from the group consisting of aluminum nitrate (Al(NO).9HO) claim 1 , aluminum chloride (AlCl.6HO) claim 1 , and aluminum acetate (CHAlO).6. The method of claim 1 , wherein the precipitant is one or more kinds of ammonia (NH) and urea (CO(NH)).7. The method of claim 1 , wherein the metal oxide precursor in the mixed solution has a concentration ranging from 50 to 2000 mM.8. The method of claim 1 , wherein the mixed solution has a pH ranging from 3 to 12.9. The method of claim 1 , wherein the precipitation step is performed at a temperature of ...

CATALYST USED FOR RESOURCE UTILIZATION OF A FIXED BED ANILINE DISTILLATION RESIDUE AND METHOD FOR PREPARING SAID CATALYST

The present invention relates to a catalyst for fixed bed aniline rectification residue recycling and preparation method thereof. Based on the total weight of the catalyst, the catalyst comprises the following components in percentage by weight: 5-40% of an active component, 2-30% of a first cocatalyst component, 10-30% of a second cocatalyst component and the balance of carrier, wherein the active component is NiO; the first cocatalyst component is one or more of Fe, Mo, Cr or Co oxide; and the second cocatalyst component is one or more of La, Zr, Y or Ce oxide. The catalyst is prepared through co-precipitation. The catalyst shows high activity and stability in the waste liquid treatment process, and can still maintain high rectification residue cracking rate after reaction of 200 hours. 1. A catalyst for fixed bed aniline rectification residue recycling , wherein said catalyst comprises the components described below based on the total weight of the catalyst:5-40 wt % of NiO as an active component,2-30 wt % of one or more selected from oxides of Fe, oxides of Mo, oxides of Cr and oxides of Co as a first cocatalyst component,10-30 wt % of one or more selected from oxides of La, oxides of Zr, oxides of Y and oxides of Ce as a second cocatalyst component,the remaining portion being the support.2. The catalyst according to claim 1 , wherein said catalyst comprises the components described below based on the total weight of the catalyst:15-30 wt % of NiO as the active component,5-25 wt % of one or more selected from oxides of Fe, oxides of Mo, oxides of Cr and oxides of Co as the first cocatalyst component,15-25 wt % of one or more selected from oxides of La, oxides of Zr, oxides of Y and oxides of Ce as the second cocatalyst component,the remaining portion being the support.3. The catalyst according to claim 1 , wherein the support is SiO.4. A method of preparing the catalyst of claim 1 , wherein said method comprises:A) dissolving nickel nitrate, the nitrates of the ...

CATALYTIC GAS PHASE FLUORINATION

The present invention relates to a fluorination process, comprising: 1. A fluorination process , comprising:an activation stage comprising contacting a fluorination catalyst with an oxidizing agent-containing gas flow for at least one hour; andat least one reaction stage comprising reacting a chlorinated compound with hydrogen fluoride in gas phase in the presence of the fluorination catalyst, so as to produce a fluorinated compound.2. The process of claim 1 , comprising a plurality of reaction stages alternating with a plurality of regeneration stages claim 1 , wherein the reaction stages comprise reacting the chlorinated compound with hydrogen fluoride in gas phase in the presence of the fluorination catalyst claim 1 , and the regeneration stages comprise contacting the fluorination catalyst with an oxidizing agent-containing gas flow.3. The process of or claim 1 , wherein the oxidizing agent-containing gas flow of the activation stage and/or the regeneration stages is an oxygen-containing gas flow.4. The process of one of to claim 1 , wherein the activation stage and/or the regeneration stages comprise contacting the fluorination catalyst with the oxidizing agent-containing gas flow for at least 2 hours claim 1 , preferably for at least 4 hours claim 1 , more preferably for at least 10 hours claim 1 , and even more preferably for at least 15 hours.5. The process of one of to claim 1 , wherein the oxidizing agent-containing gas flow of the activation stage and/or the regeneration stages contains hydrogen fluoride in addition to the oxidizing agent claim 1 , and wherein the proportion of oxidizing agent in the oxidizing agent-containing gas flow of the activation stage and/or the regeneration stages is preferably from 2 to 98 mol % claim 1 , and more preferably from 5 to 50 mol % claim 1 , relative to the total amount oxidizing agent and hydrogen fluoride.6. The process of one of to claim 1 , wherein the oxidizing agent-containing gas flow of the activation stage ...

Process for the preparation of 2,3,3,3-tetrafluoropropene

The present invention provides a process for preparing 2,3,3,3-tetrafluoropropene from 1,1,1,2,3-pentachloropropane and/or 1,1,2,2,3-pentachloropropane, comprising the following steps: (a) catalytic reaction of 1,1,1,2,3-pentachloropropane and/or 1,1,2,2,3-pentachloropropane with HF into a reaction mixture comprising HCl, 2-chloro-3,3,3-trifluoropropene, 2,3,3,3-tetrafluoropropene, unreacted HF, and optionally 1,1,1,2,2-pentafluoropropane; (b) separating the reaction mixture into a first stream comprising HCl and 2,3,3,3-tetrafluoropropene and a second stream comprising HF, 2-chloro-3,3,3-trifluoropropene and optionally 1,1,1,2,2-pentafluoropropane; (c) catalytic reaction of the second stream into a reaction mixture comprising 2,3,3,3-tetrafluoropropene, HCl, unreacted 2-chloro-3,3,3-trifluoropropene, unreacted HF and optionally 1,1,1,2,2-pentafluoropropane and (d) feeding the reaction mixture of step (c) directly without separation to step (a).

PHOTOCATALYST MATERIAL AND METHOD FOR PRODUCING SAME

A photocatalytic member comprises a base and a photocatalytic layer fixed on the base. The photocatalytic layer comprises first photocatalyst particles being visible light responsive photocatalyst particles for hydrogen generation, second photocatalyst particles being visible light responsive photocatalyst particles for oxygen generation, and conductive particles which are provided between the first photocatalyst particle and the second photocatalyst particle, have Fermi level at a negative position relative to an electronic energy level at the upper end of the valence band of the first photocatalyst particle and at a positive position relative to an electronic energy level at the bottom end of the conduction band of the second photocatalyst particle, and are able to store an electron and a hole. In the photocatalytic layer, the conductive particles are located to be coupled to both the first photocatalyst particles and the second photocatalyst particles. 1. A photocatalytic member comprising a base and a photocatalytic layer fixed on the base , wherein the photocatalytic layer comprisesfirst photocatalyst particles being visible light responsive photocatalyst particles for hydrogen generation,second photocatalyst particles being visible light responsive photocatalyst particles for oxygen generation, andconductive particles which are provided between the first photocatalyst particle and the second photocatalyst particle, have Fermi level at a negative position relative to an electronic energy level at the upper end of the valence band of the first photocatalyst particle and at a positive position relative to an electronic energy level at the bottom end of the conduction band of the second photocatalyst particle, and are able to store an electron and a hole, andwherein the conductive particles are located to be coupled to both the first photocatalyst particles and the second photocatalyst particles.2. The photocatalytic member according to claim 1 , whereinthe ...

Method for producing high-purity 1,5-pentanediol

The present invention has an object to provide a method for efficiently producing high-purity 1,5-pentanediol by reacting tetrahydrofurfuryl alcohol with hydrogen. This manufacturing method for producing high-purity 1,5-pentanediol comprises: step (I): a step of obtaining a crude reaction product by a hydrogenolysis reaction of tetrahydrofurfuryl alcohol with hydrogen carried out in the presence of a copper-containing catalyst with reaction temperature of 200 to 350° C. and reaction pressure of 1 to 40 MPa until conversion rate of tetrahydrofurfuryl alcohol reaches 80% or less; step (II): a step of separating tetrahydrofurfuryl alcohol and crude 1,5-pentanediol (A) from the crude reaction product obtained in the step (I), and then, supplying recovered tetrahydrofurfuryl alcohol as a raw material for the step (I); and step (III): a step of obtaining the high-purity 1,5-pentanediol by distillation of the crude 1,5-pentanediol (A) obtained in the step (II).

Method for producing alkanediol

Provided by the present invention is a method for producing an alkanediol, such as 1,5-pentanediol, with a high reaction selectivity thereto by reacting a cyclic ether group-containing methanol such as tetrahydrofurfuryl alcohol by using a non-chromium catalyst not containing chromium atom. More specifically, the method is to produce an alkanediol having hydroxy groups at both molecular terminals shown by the formula (2), includes reacting a cyclic ether group-containing methanol shown by the formula (1) with hydrogen in the presence of a metal catalyst which contains copper atom, at least one co-existing atom selected from the group consisting of elements of the third to the sixth periods of the II to XIV groups (excluding chromium) in the periodical table and lanthanide elements.

PROCESS FOR PRODUCING TRIMETHYLHEXAMETHYLENEDIAMINE

Trimethylhexamethylenediamine is produced by hydrogenating a trimethylhexamethylenedinitrile-comprising mixture in the presence of at least ammonia and hydrogen and a catalyst in the presence or absence of solvent, wherein the catalyst has the following properties: I. after activation the catalyst in its entirety has the following composition in weight percent (wt %), wherein the proportions add up to 100 wt %, based on the metals present: cobalt: 55 to 95 wt %, aluminum: 5 to 45 wt %, chromium: 0 to 3 wt %, and nickel: 0 to 7 wt %, and II. the catalyst is present in the form of irregular particles as granulate and after activation has particle sizes of 1 to 8 mm. 1. A process for producing trimethylhexamethylenediamine , comprising:hydrogenating a trimethylhexamethylenedinitrile-comprising mixture in the presence of at least ammonia and hydrogen and a catalyst in the presence or absence of solvent,wherein the catalyst has the following properties:I. after activation the catalyst in its entirety has the following composition in weight percent (wt %), wherein the proportions add up to 100 wt %, based on the metals present:cobalt: 55 to 95 wt %,aluminum: 5 to 45 wt %,chromium: 0 to 3 wt %, andnickel: 0 to 7 wt %, andII. the catalyst is present in the form of irregular particles as granulate and after activation has particle sizes of 1 to 8 mm.2. The process according to claim 1 , whereinI. after activation the catalyst in its entirety has the following composition in weight percent (wt %), wherein the proportions add up to 100 wt %, based on the metals present:cobalt: 55 to 90 wt %,aluminum: 5 to 44.5 wt %, andchromium: 0.5 to 5 wt %.3. The process according to claim 1 , whereinI. after activation the catalyst in its entirety has the following composition in weight percent (wt %), wherein the proportions add up to 100 wt %, based on the metals present:cobalt: 55 to 88 wt %,aluminum: 5 to 44.5 wt %, andnickel: 0.5 to 7 wt %.4. The process according to claim 1 , ...

CATALYST AND PROCESS USING THE CATALYST FOR MANUFACTURING FLUORINATED HYDROCARBONS

A catalyst comprising chromia and at least one additional metal or compound thereof and wherein the catalyst has a total pore volume of greater than 0.3 cm/g and the mean pore diameter is greater than or equal to 90 Å, wherein the total pore volume is measured by N2 adsorption porosimetry and the mean pore diameter is measured by NBET adsorption porosimetry, and wherein the at least one additional metal is selected from Li, Na, K, Ca, Mg, Cs, Sc, Al, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Re, Fe, Ru, Co, Rh, Ir, Ni, Pd, In, Pt, Cu, Ag, Au, Zn, La, Ce and mixtures thereof. 1. A catalyst comprising chromia and at least one additional metal or compound thereof and wherein the catalyst has a total pore volume of greater than 0.3 cm/g and the mean pore diameter is greater than or equal to 90 Å , wherein the total pore volume is measured by Nadsorption porosimetry and the mean pore diameter is measured by NBET adsorption porosimetry , and wherein the at least one additional metal is selected from the group consisting of: Li , Na , K , Ca , Mg , Cs , Sc , Al , Y , Ti , Zr , Hf , V , Nb , Ta , Cr , Mo , W , Mn , Re , Fe , Ru , Co , Rh , Ir , Ni , Pd , In , Pt , Cu , Ag , Au , Zn , La , Ce and mixtures thereof.2. A catalyst according to claim 1 , wherein the pore volume is equal to or greater than 0.4 cm/g.3. A catalyst according to claim 1 , wherein the average pore width of the catalyst is greater than or equal to 100 Å when measured by NBET adsorption porosimetry.4. A catalyst according to claim 1 , wherein the average pore width of the catalyst is greater than or equal to 130 Å when measured by NBJH adsorption porosimetry.5. A catalyst according to claim 1 , wherein the average pore width of the catalyst is greater than or equal to 90 Å when measured by NBJH desorption porosimetry.6. A catalyst according to provided in the form of a pellet or pellets comprising a plurality of catalyst particles.7. A catalyst according to claim 6 , wherein the pellets comprise graphite ...

CATALYTIC GAS PHASE FLUORINATION

The present invention relates to a fluorination process, comprising: 120.-. (canceled)21. A fluorination process , comprising:an activation stage comprising the following steps, in succession:i. reacting a chlorinated compound selected from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene, 1,1,1,2,3-pentachloropropane, 1,1,2,2,3-pentachloropropane, 2,3-dichloro-1,1,1-trifluoropropane, 2,3,3,3-tetrachloro-1-propene and 1,1,2,3-tetrachloro-1-propene with hydrogen fluoride in gas phase in the presence of a chromium-based fluorination catalyst, andii. contacting the chromium-based fluorination catalyst with a first oxidizing agent-containing gas flow comprising an oxidizing agent and hydrogen fluoride;at least one reaction stage comprising reacting the chlorinated compound with hydrogen fluoride in gas phase in the presence of the fluorination catalyst, so as to produce a fluorinated compound; andat least one regeneration stage comprising contacting the fluorination catalyst with a second oxidizing agent-containing gas flow.22. The process of claim 21 , wherein the first and/or second oxidizing agent-containing gas flows comprise an oxygen-containing gas flow.23. The process of claim 21 , wherein the activation stage and/or the at least one regeneration stage comprise contacting the fluorination catalyst with the first and/or second oxidizing agent-containing gas flows for at least 2 hours.24. The process of claim 21 , wherein the second oxidizing agent-containing gas flow contains hydrogen fluoride in addition to the oxidizing agent claim 21 , and wherein the proportion of oxidizing agent in the second oxidizing agent-containing gas flow is from 2 to 98 mol % claim 21 , relative to the total amount oxidizing agent and hydrogen fluoride.25. The process of claim 21 , wherein the second oxidizing agent-containing gas flow does not contain hydrogen fluoride.26. The process of claim 21 , wherein the first and/or second oxidizing agent-containing gas flow comprise ...

METHOD OF MANUFACTURING HONEYCOMB METAL STRUCTURE BY USING ALUMINUM POWDER, AND METAL CATALYST MODULE INCLUDING THE HONEYCOMB METAL STRUCTURE

Provided are a method of manufacturing a honeycomb metal structure by using aluminum (Al) powder and a metal catalyst module including the honeycomb metal structure. The method includes preparing a honeycomb structure including at least one substrate including iron (Fe), coating at least a part of the substrate with a viscid material whose viscosity is increased by moisture, attaching metal powder onto the viscid material, adhering the metal powder to the substrate by supplying the moisture to the viscid material, and generating an uneven structure made of the metal powder bonded to the substrate, by performing heat treatment of the substrate onto which the metal powder is adhered. 1. A method of manufacturing a honeycomb metal structure , the method comprising:preparing a honeycomb structure comprising at least one substrate comprising iron (Fe);coating at least a part of the substrate with a viscid material whose viscosity is increased by moisture;attaching metal powder onto the viscid material;adhering the metal powder to the substrate by supplying the moisture to the viscid material; andgenerating an uneven structure made of the metal powder bonded to the substrate, by performing heat treatment on the substrate to which the metal powder is adhered.2. The method of claim 1 , wherein the adhering of the metal powder comprises:preparing the substrate comprising the metal powder attached to the viscid material, and a container containing water;evaporating and supplying the water to the viscid material; andadhering the metal powder to the substrate due to an increase in viscosity of the viscid material.3. The method of claim 1 , wherein the heat treatment comprises:generating an intermetallic compound layer at an interface between the substrate and the metal powder by performing first heat treatment on the substrate to which the metal powder is adhered; anddissolving the intermetallic compound layer by performing second heat treatment on the first-heat-treated ...

CATALYTIC GAS PHASE FLUORINATION OF 1,1,2-TRICHLOROETHANE AND/OR 1,2-DICHLOROETHENE TO PRODUCE 1-CHLORO-2,2-DIFLUOROETHANE

The invention is directed to a catalyst for the gas phase fluorination of 1,1,2-trichloroethane and/or 1,2-dichloroethene with HF to give 1-chloro-2,2-difluoroethane which catalyst is prepared by co-depositing FeCland MgClon chromia-alumina, or co-depositing Cr(NO)and Ni(NO)on active carbon, or by doping alumina with ZnCl, and to a process for the preparation of 1-chloro-2,2-difluoroethane comprising a catalytic gas phase fluorination of 1,1,2-trichloroethane and/or 1,2-dichloroethene wherein one of the catalysts according to claim 2 or 3 is used. 1. A catalyst for gas phase fluorination of 1 ,1 ,2-trichloroethane and 1 ,2-dichloroethene with HF to give 1-chloro-2 ,2-difluoroethane which is prepared by co-depositing FeCland MgClon chromia-alumina , or co-depositing Cr(NO)and Ni(NO)on active carbon , or by doping alumina with ZnCl.2. The catalyst according to which has been fluorinated by treating the catalyst with a fluorine containing activation agent at a temperature not exceeding 400° C.3. The fluorinated catalyst according to which has been fluorinated by HF as activation agent.4. A process for preparation of 1-chloro-2 claim 2 ,2-difluoroethane comprising a catalytic gas phase fluorination of 1 claim 2 ,1 claim 2 ,2-trichloroethane comprising using a catalyst according to .5. The process according to claim 4 , wherein the ratio of catalyst weight to and flow rates of 1 claim 4 ,1 claim 4 ,2-trichloroethane and HF is in a range of 100 to 300.6. A process for preparation of 1-chloro-2 claim 2 ,2-difluoroethane comprising a catalytic gas phase fluorination of 1 claim 2 ,2-dichloroethene comprising using a catalyst according to .7. The process according to claim 6 , wherein the ratio of catalyst weight to flow rates of 1 claim 6 ,1 claim 6 ,2-trichloroethane and HF is in the range of 250 to 500.8. A process for preparation of 1-chloro-2 claim 2 ,2-difluoroethane comprising a catalytic gas phase fluorination of 1 claim 2 ,1 claim 2 ,2-trichloroethane and 1 claim 2 , ...

Process and catalyst for preparing 1,4-butanediol

The present invention relates to a process for preparing 1,4-butanediol (BDO) by hydrogenating 2-butyne-1,4-diol (BYD) or 4-hydroxybutanal (4-HBA) in the presence of a catalyst of the Raney type having a porous foam structure, wherein the macroscopic pores have sizes in the range of 100 to 5000 μm, and a bulk density of up to 0.8 kg/L.

Metal foam bodies and process for production thereof

The present invention relates to processes for producing metal foam bodies, in which metal-containing powders that may comprise aluminium and chromium or molybdenum are applied to metal foam bodies that may comprise nickel, cobalt, copper and iron and then treated thermally, wherein the highest temperature in the thermal treatment of the metal foam bodies is in the range from 680 to 715° C., and wherein the total duration of the thermal treatment within the temperature range from 680 to 715° C. is between 5 and 240 seconds. Following this method of thermal treatment can achieve alloy formation at the contact surface between metal foam body and metal-containing powder, but simultaneously leave unalloyed regions within the metal foam. The present invention further comprises processes comprising the treatment of the alloyed metal foam bodies with basic solution. The present invention further comprises the metal foam bodies obtainable by these processes, which find use, for example, as support and structure components and in catalyst technology.

Selective nickel based hydrogenation catalyst and the preparation thereof

A selective nickel-based hydrogenation catalyst and the preparation thereof, characterized in that: provided that the catalyst is weighed 100%, it comprises nickel oxide 14-20% as active component, lanthanum oxide and/or cerium oxide 2-8%, and VIB element oxide 1-8% as aids, 2-8% silica, 1-8% alkaline earth metal oxides, and alumina as the balance. The catalyst specific surface area is 60-150 m 2 /g, and the pore volume is 0.4-0.6 ml/g. The catalyst has good hydrogenation performance, especially impurity and colloid resistance and hydrogenation stability. The catalyst can be applied to the diolefin selective hydrogenation of medium or low-distillate oil, especially of the full-distillates pyrolysis gasoline.

METAL SUBSTRATE FOR CATALYTIC CONVERTER AND CATALYST CARRIER

A base for supporting a catalyst for exhaust gas purification, the base including a honeycomb structure obtained by superposing a metallic flat foil and a metallic wavy foil, characterized in that the wavy foil has offset portions where any adjoining two of the wave phases arranged in the axial direction of the honeycomb structure are offset from each other. The base is further characterized in that an oxide coating film has been formed in a given range of these offset portions which includes exposed edge surfaces that are exposed on the gas-inlet side, that the oxide coating film includes 30-99.9 mass % first alumina, with the remainder comprising at least one of second aluminas, Fe oxides, and Cr oxides, that the first alumina comprises α-alumina, that the second aluminas comprise one or more of γ-, θ-, χ-, δ-, η-, and κ-aluminas. 1. A metal substrate for catalytic converter for purifying exhaust gas , the metal substrate comprising a honeycomb core including a flat metal foil and a corrugated metal foil , the flat metal foil and the corrugated metal foil being layered , whereinthe corrugated foil has an offset part having different wave phases between front and rear in an axial direction of the honeycomb core,the offset part has an oxide film formed on an exposed end surface that is exposed toward at least a gas inlet side,the oxide film contains 30% by mass or more and 99.9% by mass or less of a first alumina with the balance comprising at least one of a second alumina, a Fe oxide, and a Cr oxide,the first alumina comprises α-alumina, andthe second alumina comprises at least one or more of γ, θ, χ, δ, η, and κ aluminas.2. The metal substrate for catalytic converter according to claim 1 , wherein a content of Fe contained in the oxide film is 0.1% by mass or more and 7% by mass or less.3. The metal substrate for catalytic converter according to claim 1 , wherein a content of Cr contained in the oxide film is 0.1% by mass or more and 4% by mass or less.4. The ...

METHOD OF MANUFACTURING OPEN-CELL BODIES AND BODIES MANUFACTURED USING SAID METHOD

In the method in accordance with the invention of manufacturing an open-cell body from a metal or ceramic material, a procedure is followed such that individual parts of an open pore plastic in a size which corresponds to the size of the bodies to be manufactured while taking account of the shrinkage on a sintering or an open pore plastic element having predetermined break points which take account of the size and geometrical design of bodies to be manufactured while considering the shrinkage in the sintering are/is infiltrated and coated with a suspension in which, in addition to a liquid, at least one powdery material is contained with which the bodies are manufactured. Organic components are expelled after a first heat treatment. Subsequently, a sintering is carried out in which open-cell bodies are obtained, wherein the parts of porous plastic provided with the suspension are separated before the first heat treatment and/or sintering or wherein, after the sintering, the open-cell element which is obtained from the plastic element from the material with which the bodies are formed is cut by forces acting at the desired break points and thereby bodies can be obtained which are present in separated form. 1. A method of manufacturing an open-cell body from a metal or ceramic material , wherein individual parts of an open pore plastic in a size which corresponds to the size of the bodies to be manufactured while taking account of the shrinkage on a sintering or{'b': 1', '2, 'an open pore plastic element () having predetermined break points () which take account of the size and geometrical design of bodies to be manufactured while considering the shrinkage in the sintering'}are/is infiltrated and coated with a suspension in which, in addition to a liquid, at least one powdery material is contained with which the bodies are manufactured; andorganic components are expelled after a first heat treatment, and subsequentlya sintering is carried out in which open-cell bodies ...

Process and apparatus for co-producing cyclohexanol and alkanol

This invention relates to a process for co-producing cyclohexanol and alkanol, including a cyclohexene esterification step and a cyclohexyl ester hydrogenation step. This invention further relates to a process for further producing cyclohexanone or caprolactam, starting from the co-producing process, and an apparatus for co-producing cyclohexanol and alkanol. The process for co-producing cyclohexanol and alkanol of this invention is environment-friendly, with low production cost and highly improved atom economy.

PISTON WITH ADVANCED CATALYTIC ENERGY RELEASE

A piston capable of reducing undesirable “knock,” reducing hydrocarbon emissions, and providing more complete combustion, is provided. The piston includes a multilayer coating having a thickness of 500 microns or less disposed on an upper combustion surface. The coating includes a bond layer including nickel disposed on the upper combustion surface. A thermal barrier layer including a ceramic composition is disposed on the bond layer. A sealant layer formed of metal is disposed on the thermal barrier layer. A catalytic layer including at least one of platinum, ruthenium, rhodium, palladium, osmium, and iridium is disposed on the sealant layer. The catalytic layer can be disposed on select regions or the entire upper combustion surface to promote combustion through a catalyzed reaction.

CATALYST COMPOSITION FOR CONVERSION OF ALKANES TO ALKENES AND METHOD OF PREPARATION THEREOF

The present invention relates to preparation of catalyst for production of olefinic hydrocarbons by dehydrogenation of their corresponding paraffins, particularly propylene from propane, comprising a metal oxide or combination of metal oxides utilizing spent catalyst from Fluid Catalytic Cracking (FCC)/Resid Fluid Catalytic Cracking (RFCC) processes. The metal oxides are possibly from transition metal group, particularly from groups VB, VIB, VIII, and Lanthanide series, and at least one metal from alkali group. The catalyst support used is spent catalyst or modified spent catalyst or combination thereof. The said catalyst can be used for both non-oxidative Propane Dehydrogenation (PDH) and Oxidative Propane Dehydrogenation (OPDH) process in the presence of CO. 1. A process for production of a catalyst for dehydrogenation of alkanes to alkenes , the process comprising:(a) obtaining spent catalyst from a refining process,(b) calcining the spent catalyst to remove coke and/or any other volatile material,(c) optionally grinding the spent catalyst to obtain spent catalyst support,(d) providing a metal solution by mixing the desired metal containing compound (s) with a solvent,(e) treating the spent catalyst or spent catalyst support with the metal solution to obtain a wet catalyst mixture or wet catalyst particles,(f) drying the wet catalyst mixture or wet catalyst particles to obtain dry catalyst mixture or dry catalyst particles,(g) optionally repeating the steps (e) and (f), and(h) calcining the dry catalyst mixture or dry catalyst particles to obtain the catalyst.2. The process according to claim 1 , wherein the refining process is fluid catalytic cracking process claim 1 , resid fluid catalytic cracking process claim 1 , high severity fluid catalytic cracking process claim 1 , high severity propylene maximizing fluid catalytic cracking process claim 1 , hydro processing claim 1 , isomerisation process or any other refinery process.3. The process according to claim 1 ...

Method For Producing Aryl-Functional Silanes

A method for preparing a reaction product including an aryl-functional silane includes sequential steps (1) and (2). Step (1) is contacting, under silicon deposition conditions, (A) an ingredient including (I) a halosilane such as silicon tetrahalide and optionally (II) hydrogen (H); and (B) a metal combination comprising copper (Cu) and at least one other metal, where the at least one other metal is selected from the group consisting of gold (Au), cobalt (Co), chromium (Cr), iron (Fe), magnesium (Mg), manganese (Mn), nickel (Ni), palladium (Pd), and silver (Ag); thereby forming a silicon alloy catalyst comprising Si, Cu and the at least one other metal. Step (2) is contacting the silicon alloy catalyst and (C) a reactant including an aryl halide under silicon etching conditions. 1. A method for preparing a reaction product comprising an aryl-functional silane comprises sequential steps (1) and (2) , where: [{'sub': a', '(4-a)', '2, '(A) an ingredient comprising (I) a halosilane of formula HSiX, where each X is independently a halogen atom, and 0≦a≦1; and optionally (II) H, with the proviso that when a=0, then the hydrogen is present; and'}, '(B) a metal combination comprising copper and at least one other metal, where the at least one other metal is selected from the group consisting of gold, cobalt, chromium, iron, magnesium, manganese, nickel, palladium, and silver; thereby forming a silicon alloy catalyst comprising silicon, copper and the at least one other metal; and, 'step (1) is contacting, under silicon deposition conditions'}step (2) is contacting the silicon alloy catalyst and (C) a reactant comprising an aryl halide under silicon etching conditions; thereby forming the reaction product, where the reaction product comprises the aryl-functional silane and a spent catalyst;where the method may optionally further comprise step (3) and step (4), where{'sub': a', '(4-a)', '2, 'step (3) is contacting, under silicon deposition conditions, an additional ...

Catalytic and sorptive articles comprising metal fiber felt substrates

Catalytic and/or sorptive articles comprising a metal fiber felt, the metal felt having an array of metal fibers and voids and a catalyst composition and/or a sorbent composition disposed on the metal fibers and within the voids are described. Such articles can be highly effective towards the abatement of pollutants in exhaust gas streams from internal combustion engines.

PROCESS FOR PREPARING 3-AMINOMETHYL-3,5,5-TRIMETHYLCYCLOHEXYLAMINE

Isophoronediamine, is prepared by A) subjecting isophoronenitrile directly in one stage to aminating hydrogenation to give isophoronediamine in the presence of ammonia, hydrogen, a hydrogenation catalyst and an optional additive, and in the presence or absence of an organic solvent; or B) first converting isophoronenitrile fully or partly in at least two or more than two stages to isophoronenitrile imine, and subjecting the isophoronenitrile imine to aminating hydrogenation to give isophoronediamine as a pure substance or in a mixture with another component and/or isophoronenitrile, in the presence of at least ammonia, hydrogen and a catalyst. 1. A process for preparing isophoronediamine , comprising:A) subjecting isophoronenitrile directly in one stage to aminating hydrogenation to give isophoronediamine in the presence of ammonia, hydrogen, a hydrogenation catalyst and an optional additive, and in the presence or absence of an organic solvent;or 'wherein the aminating hydrogenation proceeds in the presence of at least ammonia, hydrogen and a catalyst:', 'wherein isophoronenitrile is first converted fully or partly to isophoronenitrile imine, and the isophoronenitrile imine is subjected to aminating hydrogenation to give isophoronediamine as a pure substance or in a mixture with another component and/or isophoronenitrile,'}, 'B) converting isophoronenitrile to isophoronediamine in at least two or more than two stages,'}wherein the catalyst has, after catalyst activation, in its entirety, the following composition in percent by weight (% by weight), wherein the proportions add up to 100% by weight, based on the metals present:cobalt: 55% to 95% by weight,aluminium: 5% to 45% by weight,chromium: 0% to 3% by weight, andnickel: 0% to 7% by weight; andwherein the catalyst is in the form of hollow spheres having a diameter of 1 to 8 mm.2. The process for preparing isophoronediamine according to claim 1 , wherein the catalyst has claim 1 , after catalyst activation claim ...

METHODS, SYSTEMS AND DEVICES FOR SIMULTANEOUS PRODUCTION OF LACTIC ACID AND PROPYLENE GLYCOL FROM GLYCEROL

Methods, processes and systems for using solid catalysts to simultaneously produce lactic acid and propylene glycol from glycerol are provide, as are methods, processes and systems of converting glycerol use heterogeneous catalytic agents. Different combinations of catalysts and reaction conditions provide tunable ranges for the yields of lactic acid and propylene glycol. The conversion methods, processes and systems are not reliant on external hydrogen. Applications to crude glycerol, including that co-produced during biodiesel production, are also described. 1. A method of converting glycerol to lactic acid , propylene glycol or a combination thereof , the method comprising:providing liquid glycerol;providing a heterogeneous catalyst, wherein the heterogeneous catalyst comprises a base ingredient and a dehydrogenation ingredient, wherein the base ingredient comprises an alkaline earth metal oxide selected from the group consisting of magnesium oxide (MgO), calcium oxide (CaO), and strontium oxide (SrO);reacting the liquid glycerol with the heterogeneous catalyst,whereby glycerol is converted to a product comprising lactic acid, propylene glycol or a combination thereof.2. The method of claim 1 , wherein reacting the liquid glycerol with the heterogeneous catalyst causes simultaneous production of lactic acid and propylene glycol.3. (canceled)413. The method of claim claim 1 , wherein the dehydrogenation ingredient comprises a metal catalyst.5. The method of claim 4 , wherein the metal catalyst is selected from the group consisting of copper (Cu) claim 4 , cuprous oxide (CuO) claim 4 , copper oxide (CuO) claim 4 , copper chromite (CuCrO) claim 4 , barium promoted copper chromite (Ba—CuCrO) and copper ore.67-. (canceled)8. The method of claim 1 , wherein the base ingredient and dehydrogenation ingredient of the heterogeneous catalyst are mixed or wherein the dehydrogenation ingredient is supported on the base ingredient.9. The method of claim 8 , wherein the ...

METHOD FOR PRODUCING HYDRIDE USING UNSATURATED COMPOUND HAVING CARBON NUMBER OF 4 AS RAW MATERIAL

The present invention relates to a method for producing a hydride having a carbon number of 4, comprising contacting, in liquid phase, an unsaturated compound having a carbon number of 4 as a raw material with a solid catalyst obtained by loading a metal element belonging to Groups 9 to 11 of the long periodic table on a support, thereby performing hydrogenation to produce a corresponding hydride having a carbon number of 4, wherein hydrogenation is performed in the presence of, as a solvent, a 1,4-butanediol having a nitrogen component concentration of 1 ppm by weight to 1 wt % in terms of nitrogen atom. 1. A method for producing a hydride having a carbon number of 4 , comprising contacting , in liquid phase , an unsaturated compound having a total carbon number of 4 as a raw material with a solid catalyst obtained by loading a metal element belonging to Groups 9 to 11 of the long periodic table on a support , and performing hydrogenation to continuously produce a corresponding hydride having a carbon number of 4 , wherein the hydrogenation is performed in the presence of , a solvent comprising 1 ,4-butanediol having a nitrogen component concentration of 1 ppm by weight to 1 wt % in terms of nitrogen atom.2. The method for producing a hydride having a carbon number of 4 according to claim 1 , wherein the 1 claim 1 ,4-butanediol is previously contacted with an anion exchange resin to adjust the nitrogen concentration in the 1 claim 1 ,4-butanediol to be from 1 ppm by weight to 1 wt %.3. The method for producing a hydride having a carbon number of 4 according to claim 1 , wherein the support is at least one member of silica and diatomaceous earth.4. The method for producing a hydride having a carbon number of 4 according to claim 1 , wherein the unsaturated compound having a carbon number of 4 is 1 claim 1 ,4-dihydroxy-2-butene and the corresponding hydride having a carbon number of 4 is at least one member of 2 claim 1 ,-hydroxytetrahydrofuran and 1 claim 1 ,4- ...

CATALYST FOR OXIDATIVE DEHYDROGENATION AND METHOD OF PREPARING THE SAME

Disclosed are a catalyst for oxidative dehydrogenation and a method of preparing the same. More particularly, a catalyst for oxidative dehydrogenation of butene having a high butene conversion rate and superior side reaction inhibition effect and thus having high reactivity and high selectivity for a product by preparing metal oxide nanoparticles and then fixing the prepared metal oxide nanoparticles to a support, and a method of preparing the same are provided. 1. A catalyst for oxidative dehydrogenation , comprising a metal oxide having a composition represented by Formula 1 below and an average particle diameter of 0.1 to 50 nm; and a support:{'br': None, 'sub': 2', '4, 'ABO\u2003\u2003[Formula 1]'}wherein A is one or more selected from the group consisting of divalent cationic metals and B is one or more selected from the group consisting of trivalent cationic metals.2. The catalyst according to claim 1 , wherein A is one or more selected from the group consisting of Cu claim 1 , Ra claim 1 , Ba claim 1 , Sr claim 1 , Ca claim 1 , Cu claim 1 , Be claim 1 , Fe(II) claim 1 , Zn claim 1 , Mg claim 1 , Mn claim 1 , Co claim 1 , and Ni.3. The catalyst according to claim 1 , wherein B is one or more selected from the group consisting of Al claim 1 , Fe(III) claim 1 , Cr claim 1 , Si claim 1 , V claim 1 , Ga claim 1 , In claim 1 , La claim 1 , and Ce.4. The catalyst according to claim 1 , wherein the metal oxide is comprised in an amount of 1 to 40 parts by weight based on 100 parts by weight of the support.5. The catalyst according to claim 1 , wherein the support comprises one or more selected from the group consisting of alumina claim 1 , silica claim 1 , cordierite claim 1 , titania claim 1 , zirconia claim 1 , silicon nitride claim 1 , and silicon carbide.6. The catalyst according to claim 1 , wherein the catalyst is a supporting catalyst or a coating catalyst.7. A method of preparing a catalyst for oxidative dehydrogenation claim 1 , wherein the method is ...

EXHAUST GAS TREATMENT CATALYST

An exhaust gas treatment catalyst comprises titanium oxide, tungsten oxide, vanadium oxide, and copper oxide and/or Cu/zeolite-coated catalyst, wherein the catalyst is provided with a nitrogen oxide removing capability in which nitrogen oxides contained in an exhaust gas are subjected to catalytic reduction in the presence of ammonia, and with CO and VOC removing capability. 1. An exhaust gas treatment catalyst comprising titanium oxide , tungsten oxide , vanadium oxide , and copper oxide and/or a Cu/zeolite-coated catalyst , wherein the catalyst has a nitrogen oxide removing capability in which nitrogen oxides contained in an exhaust gas are subjected to catalytic reduction in the presence of ammonia , and with CO and VOC removing capability.2. The exhaust gas treatment catalyst according to claim 1 , wherein the copper oxide is present in an amount of 0.2 to 0.75 wt %.3. The exhaust gas treatment catalyst according to claim 1 , wherein the Cu/zeolite-coated catalyst is present in an amount of 50 g to 200 g/mas coating over the base material. 1. Technical FieldThe present invention relates to an exhaust gas treatment catalyst.2. Background ArtNOx carbon monoxide (CO), volatile organic compounds (VOC) such as saturated hydrocarbons excluding methane and ethane, and unsaturated hydrocarbons such as ethylene, and the like are present in exhaust gases discharged from various industrial devices, for example, automobile engines, gas engines, gas turbines for aircraft and power generation, chemical plants, various factories, and the like.Expensive oxidation catalysts prepared by using platinum (Pt) are used as exhaust gas treatment materials in order to remove CO and VOC in addition to reducing NOx.Proposed in, for example, patent document 1 (Japanese Patent No. 4939082) is an exhaust gas treatment system in which for the purpose of reducing as discharge amount of CO in an exhaust gas treatment facility, noble metals are added to a denitration catalyst in a front stage to ...

METHOD FOR PRODUCING ETHANOL AND COPRODUCING METHANOL

A method for producing ethanol and coproducing methanol on a catalyst in a reactor using a co-feed of a synthesis gas and acetate as a reaction raw material comprising passing a raw material gas containing an acetate and a synthesis gas through a reactor loaded with a catalyst to produce ethanol and coproduce methanol under conditions of a reaction temperature of 150-350° C., a reaction pressure of 0.1-20.0 MPa, a reaction volume hourly space velocity of 100-45000 mlgh, and an acetate weight hourly space velocity of 0.01-5.0 h; and the active components of the catalyst are copper and optionally zinc and/or aluminum, which greatly facilitates the conversion of carbon monoxide to methanol, while an extremely high activity of acetate hydrogenation is maintained. 1. A method for producing ethanol and coproducing methanol , comprising passing a raw material gas containing an acetate and a synthesis gas through a reactor loaded with a catalyst to produce ethanol and coproduce methanol under conditions of a reaction temperature of 150-350° C. , a reaction pressure of 0.1-20.0 MPa , a reaction volume hourly space velocity of 100-45000 mlgh , and an acetate weight hourly space velocity of 0.01-5.0 h; and the active components of the catalyst are copper and optionally zinc and/or aluminum.2. The method according to claim 1 , wherein the acetate is methyl acetate and/or ethyl acetate.3. The method according to claim 1 , wherein in the catalyst claim 1 , the active component copper comprises 50.0-100.0 wt % of the total weight of the catalyst in terms of CuO; the active component zinc comprises 0-35.0 wt % of the total weight of the catalyst in terms of ZnO; and the active component aluminum comprises 0-10.0 wt % of the total weight of the catalyst in terms of AlO.4. The method according to claim 1 , wherein the catalyst further contains one or more of manganese claim 1 , molybdenum claim 1 , zirconium claim 1 , chromium claim 1 , iron claim 1 , barium claim 1 , magnesium claim ...

INDUCTION HEATED AROMATIZATION OF HIGHER HYDROCARBONS

A reactor system for aromatization of higher hydrocarbons within a given temperature range T upon bringing a reactant stream including higher hydrocarbons into contact with a catalytic mixture. The reactor system includes a reactor unit arranged to accommodate a catalytic mixture. The catalytic mixture includes a catalyst material and a ferromagnetic material. The catalyst material is arranged to catalyze the aromatization of higher hydrocarbons. The ferromagnetic material is ferromagnetic at least at temperatures up to an upper limit of the given temperature range T, where the temperature range T is the range from between about 400° C. and about 700° C. or a subrange thereof. The reactor system also includes an induction coil arranged to be powered by a power source supplying alternating current, whereby the ferromagnetic material is heated to a temperature within the temperature range T by means of an alternating magnetic field.

Method for Producing 1,3,3,3-Tetrafluoropropene

Provided is a method for causing a dehydrofluorination reaction of 1,1,1,3,3-pentafluoropropane in the gas phase and in the presence of a catalyst thereby producing 1,3,3,3-tetrafluoropropene. In this method, the reaction is carried out at a pressure inside the reaction system of from 0.001 to 90 kPa (absolute pressure) at a reaction temperature ranging from 250 to 600° C. 1. A method for producing 1 ,3 ,3 ,3-tetrafluoropropene , characterized by comprising the steps of:causing a dehydrofluorination reaction of 1,1,1,3,3-pentafluoropropane in the gas phase and in the presence of a catalyst thereby producing 1,3,3,3-tetrafluoropropene,wherein the reaction is carried out at a pressure inside the reaction system of from 0.001 to 90 kPa (absolute pressure) at a reaction temperature ranging from 250 to 600° C.2. A production method as claimed in claim 1 , wherein the catalyst is a metal compound-carried catalyst where a metal compound is carried on a metal oxide or activated carbon claim 1 , or a metal oxide.3. A production method as claimed in claim 2 , wherein the metal compound comprises at least one kind selected from the group consisting of aluminum claim 2 , titanium claim 2 , chromium claim 2 , manganese claim 2 , nickel claim 2 , copper claim 2 , cobalt claim 2 , zirconium claim 2 , niobium claim 2 , molybdenum claim 2 , tin claim 2 , antimony and tantalum.4. A production method as claimed in claim 2 , wherein the metal oxide is at least one kind selected from the group consisting of alumina claim 2 , zirconia claim 2 , titania and magnesia.5. A production method as claimed in claim 2 , wherein the metal compound is a metal halide or a metal oxyhalide.6. A production method as claimed in claim 2 , wherein the metal oxide is obtained by a modification treatment with hydrogen fluoride claim 2 , hydrogen chloride or a chlorinated and fluorinated hydrocarbon.7. A production method as claimed in claim 1 , further comprising the steps of:separating and removing ...

CATALYTIC GAS PHASE FLUORINATION

The invention relates to a fluorination process, alternately comprising reaction stages and regeneration stages, wherein the reaction stages comprise reacting a chlorinated compound with hydrogen fluoride in gas phase in the presence of a fluorination catalyst to produce a fluorinated compound, and the regeneration stages comprise contacting the fluorination catalyst with an oxidizing agent-containing gas flow. 120-. (canceled)21. A process for producing 2 ,3 ,3 ,3-tetrafluoropropene or 2-chloro-3 ,3 ,3-trifluoropropene , comprising:drying a fluorination catalyst, and i) contacting the fluorination catalyst with hydrogen fluoride; and', 'ii) optionally contacting the fluorination catalyst with an oxidizing agent-containing gas flow; and, 'activating the fluorination catalyst byreacting 1,1,1,2,3-pentachloropropane with hydrogen fluoride in the gas phase in the presence of the activated fluorination catalyst, so as to produce 2-chloro-3,3,3-trifluoro-1-propene; orreacting 1,1,2,3-tetrachloropropene or 2,3,3,3-tetrachloropropene with hydrogen fluoride in the gas phase in the presence of the activated fluorination catalyst, so as to produce 2-chloro-3,3,3-trifluoro-l-propene or 2,3,3,3-tetrafluoropropene, andregenerating the fluorination catalyst by contacting it with an oxidizing agent-containing gas flow.22. The process of claim 21 , wherein the activation stage and the reaction stage take place in a single reactor.23. The process of claim 21 , wherein step i) further comprises claim 21 , contacting the fluorination catalyst with 2-chloro-3 claim 21 ,3 claim 21 ,3-trifluoro-1-propene; 1 claim 21 ,1 claim 21 ,1 claim 21 ,2 claim 21 ,3 -pentachloropropane; 1 claim 21 ,1 claim 21 ,2 claim 21 ,3-tetrachloropropene; or 2 claim 21 ,3 claim 21 ,3 claim 21 ,3 -tetrachloropropene.24. The process of claim 21 , wherein the oxidizing agent-containing gas flow of the regeneration stage is an oxygen-containing gas flow.25. The process of claim 21 , wherein the regeneration stage ...

ELECTRO-LESS PRODUCTION OF SILICON NANOWIRES AND PLATES IN A SOLUTION

A composition and method for creating silicon nanowires or silicon nano-plates is presented, the composition comprising: Potassium Hydroxide (KOH), at least one catalyst, Sodium Metal Siliconate (NaSiO), and Ethylenediaminetetraacetic Acid (EDTA), which act as a first chelating agent. 2. The composition of claim 1 , wherein the catalyst is at least one metallic compound possessing metallic characteristics.3. The composition of claim 1 , further comprises Sodium Diehyldithiocarbamat (CHNSNa) claim 1 , which acts as a second chelating agent.4. The composition of claim 1 , further comprises a short organic compound claim 1 , which acts as a buffer that is able to regulate the amount of silicon nanowires or plates formed and to prevent agglomeration.5. The composition of claim 3 , wherein the ratio between the EDTA and the Sodium Diethyldithiocarbamate determines the nanowires structure formed in the solution e.g. long and thin nanowires or short and thick nanowires.6. (canceled)7. The composition of claim 4 , wherein the short organic compound is Dimethylacrylic Acid.8. The composition of claim 2 , wherein the metallic compound comprises gold claim 2 , silver claim 2 , cooper claim 2 , stainless steel or a combination thereof.9. The composition of claim 2 , wherein the metallic compound is a mesh.10. (canceled)11. A method for creating a solution enabling the production of silicon nanowires or silicon nano-plates claim 2 , said method comprising:introducing into a basin distilled water;introducing into said solution Potassium Hydroxide (KOH), which acts as an electron mediator;forming a homogenized solution;warming said solution up to 75 degrees Celsius and keeping the solution below boiling point;introducing into said solution at least one catalyst;introducing into said solution Sodium Methyl Siliconate;introducing into said solution Ethylenediaminetetraacetic Acid (EDTA), which acts as a first chelating agent;{'sub': 5', '10', '2, 'introducing into said solution ...

PROCESS FOR THE PREPARATION OF 2,3,3,3-TETRAFLUOROPROPENE

The present invention provides a process for preparing 2,3,3,3-tetrafluoropropene from 1,1,1,2,3-pentachloropropane and/or 1,1,2,2,3-pentachloropropane, comprising the following steps: (a) catalytic reaction of 1,1,1,2,3-pentachloropropane and/or 1,1,2,2,3-pentachloropropane with HF into a reaction mixture comprising HCl, 2-chloro-3,3,3-trifluoropropene, 2,3,3,3-tetrafluoropropene, unreacted HF, and optionally 1,1,1,2,2-pentafluoropropane; (b) separating the reaction mixture into a first stream comprising HCl and 2,3,3,3-tetrafluoropropene and a second stream comprising HF, 2-chloro-3,3,3-trifluoropropene and optionally 1,1,1,2,2-pentafluoropropane; (c) catalytic reaction of the second stream into a reaction mixture comprising 2,3,3,3-tetrafluoropropene, HCl, unreacted 2-chloro-3,3,3-trifluoropropene, unreacted HF and optionally 1,1,1,2,2-pentafluoropropane and (d) feeding the reaction mixture of step (c) directly without separation to step (a). 110.-. (canceled)11. A process for producing 2 ,3 ,3 ,3-tetrafluoropropene , comprising(a) in a first reaction zone, reacting 1,1,1,2,3-pentachloropropane and/or 1,1,2,2,3-pentachloropropane with HF in the presence of a catalyst to produce a first reaction mixture comprising HCl, 2-chloro-3,3,3-trifluoropropene, 2,3,3,3-tetrafluoropropene, unreacted HF and optionally 1,1,1,2,2-pentafluoropropane, wherein the catalyst comprises a supported or unsupported catalyst containing at least one metal selected from the group consisting of Cr, Ni, Fe, Zn, Ti, V, Zr, Mo, Ge, Sn, Pb, Mg, Sb, Co, Ru, Rh, Pd, Os, Ir, Pt, Mn, Re, Sc, Y, La, Hf, Cu, Ag, Au, and metals having an atomic number of 58 through 71;(b) separating the first reaction mixture into a first stream and a second stream comprising 2-chloro-3,3,3-trifluoropropene;(c) in a second reaction zone, reacting HF and the second stream in the presence of a catalyst in a gas phase to produce a second reaction mixture comprising 2,3,3,3-tetrafluoropropene, HCl, unreacted 2-chloro-3,3, ...

MIXED METAL OXIDE CATALYST AND PRODUCTION OF NITRIC OXIDE BY OXIDATION OF AMMONIA

The present invention provides a catalyst for production of nitric oxide from ammonia and oxygen. The catalyst has the composition ABO, wherein A and B are selected from the group Mn, Co, Cr, Fe and Al, x is between 0 and 3 and y is between 0 and 6. The catalyst has a high selectivity towards nitric oxide and a low ignition temperature in the reactor. Further the present invention relates to a method for the production of gas comprising nitric oxide by the catalyst of the present invention. The produced gas has a low content of nitrous oxide. 110-. (canceled)11. A method for the production of a gas comprising nitric oxide , the method comprising:{'sub': c', '3-x', 'x', '4, 'converting a gas blend comprising ammonia and oxygen in a reactor at a reactor temperature Tof 800 to 950° C. in the presence of a catalyst comprising the composition ABO, wherein a combination of A and B are selected fromA=Mn or Cr and B=Co, and0 Подробнее

CATALYST COMPOSITION FOR EXHAUST GAS PURIFICATION AND CATALYST FOR EXHAUST GAS PURIFICATION

The invention relates to a catalyst composition using other metals different from precious metals as a catalytically active component and is to propose a novel catalyst composition for exhaust gas purification which has excellent catalytic activity, in particular, excellent treatment activity of HC even after a thermal durability treatment. The invention is to propose a catalyst composition for exhaust gas purification comprising catalyst particles having a constitution in which Cu and a transition metal A including at least one of Cr, Fe, Mn, Co, Ni, Zr, and Ag are supported on ceria (CeO) particles and a catalyst using the same. 1. A catalyst composition for exhaust gas purification comprising catalyst particles having a constitution in which Cu and a transition metal A including at least one of Cr , Fe , Mn , Co , Ni , Zr , and Ag are supported on ceria (CeO) particles , wherein the Cu and the transition metal A of the catalyst particles are supported on the ceria (CeO) particles in a state of being capable of being changed into a delafossite-type oxide when being heated under a reducing atmosphere.2. A catalyst composition for exhaust gas purification containing catalyst particles having a constitution in which Cu and a transition metal A including at least one of Cr , Fe , Mn , Co , Ni , Zr , and Ag are supported on ceria (CeO) particles , wherein the Cu and the transition metal A of the catalyst particles are supported on the ceria (CeO) particles in a state of an each oxide or a metal or in a state of a composite oxide thereof , and{'sub': '2', 'the Cu and the transition metal A of the catalyst particles are supported on the ceria (CeO) particles in a state of being capable of being changed into a delafossite-type oxide when being heated under a reducing atmosphere.'}3. (canceled)4. The catalyst composition for exhaust gas purification according to claim 1 , wherein the transition metal A is contained in a ratio of 0.05 to 20 mass % with respect to the ...

CATALYTIC METAL FIBER FELT AND ARTICLES MADE THEREFROM

The invention provides a metal fiber felt including a woven or nonwoven mixture of fibers including a first plurality of core/shell catalytic metal fibers and an optional second plurality of reinforcing fibers, wherein the catalytic metal fibers include a core including a first metal and a shell including a catalytic metal, the catalytic metal being a noble metal, a base metal, or a combination thereof, and wherein the average diameter of the reinforcing fibers, when present, is greater than the average diameter of the catalytic metal fibers. The metal fiber felt is useful in catalytic articles for use in the abatement of pollutants in exhaust gas streams from internal combustion engines and other environmental and/or chemical catalytic processes.

EXHAUST GAS PURIFICATION CATALYST

Provided is a novel exhaust gas purification catalyst, which uses a Cu-based delafossite oxide, capable of increasing the exhaust gas purification performance compared to the case of using the Cu-based delafossite oxide alone. Proposed is an exhaust gas purification catalyst comprising a delafossite-type oxide represented by a general formula ABOand an inorganic porous material, wherein Cu is contained in the A site of the general formula of the delafossite oxide, one or two or more elements selected from the group consisting of Mn, Al, Cr, Ga, Fe, Co, Ni, In, La, Nd, Sm, Eu, Y, V, and Ti are contained in the B site thereof, and Cu is contained in 3 to 30% relative to the total content (mass) of the delafossite-type oxide and the inorganic porous material. 1. An exhaust gas purification catalyst , comprising a delafossite-type oxide represented by a general formula ABOand an inorganic porous material ,wherein Cu is comprised in the A site of the general formula of the delafossite-type oxide, one or two or more elements selected from the group consisting of Mn, Al, Cr, Ga, Fe, Co, Ni, In, La, Nd, Sm, Eu, Y, V, and Ti are comprised in the B site thereof, andCu is comprised in 3 to 30% relative to the total content (mass) of the delafossite-type oxide and the inorganic porous material.2. The exhaust gas purification catalyst according to claim 1 , wherein the content (mass) ratio of the delafossite-type oxide to the inorganic porous material is 10:90 to 70: 30.3. The exhaust gas purification catalyst according to claim 1 , wherein the ratio of an average particle diameter (D50) of the delafossite-type oxide to the average particle diameter (D50) of the inorganic porous material is 10:90 to 85:15.4. The exhaust gas purification catalyst according to claim 1 , wherein one or two or more elements selected from the group consisting of Mn claim 1 , Al claim 1 , Cr claim 1 , and Ga are comprised in the B site of the general formula.5. The exhaust gas purification catalyst ...

WATER GAS SHIFT PROCESS

A process is described for increasing the hydrogen content of a synthesis gas mixture comprising hydrogen, carbon oxides and steam, comprising the steps of: passing the synthesis gas mixture at an inlet temperature in the range 170-500° C. over a water-gas shift catalyst to form a hydrogen-enriched shifted gas mixture, wherein the water-gas shift catalyst is in the form of a cylindrical pellet having a length C and diameter D, wherein the surface of the cylindrical pellet has two or more flutes running along its length, said cylinder having no through-holes and domed ends of lengths A and B such that (A+B+C)/D is in the range 0.25 to 0.25, and (A+B)/C is in the range 0.03 to 0.30. 1. A process for increasing the hydrogen content of a synthesis gas mixture comprising hydrogen , carbon oxides and steam , the process comprising the steps of:passing the synthesis gas mixture at an inlet temperature in the range of from 170° C. to 500° C. over a water-gas shift catalyst to form a hydrogen-enriched shifted gas mixture, wherein the water-gas shift catalyst is in the form of a cylindrical pellet having a cylindrical portion length C and diameter D, wherein the surface of the cylindrical pellet has two or more flutes running along its length, said cylinder having no through-holes and domed ends of lengths A and B such that the overall length/diameter ratio (A+B+C)/D is in the range 0.25 to 1.25, and (A+B)/C is in the range of from 0.03 to 0.3.2. The process according to claim 1 , wherein the synthesis gas is derived by catalytic steam reforming claim 1 , autothermal reforming or secondary reforming a hydrocarbon or gasifying coal claim 1 , petroleum coke or biomass.3. The process according to claim 1 , wherein the carbon monoxide content of the synthesis gas is in the range of from 3 to 70 mole % on a dry-gas basis.4. The process according to claim 1 , wherein the total steam: synthesis gas volume ratio in the synthesis gas mixture is in the range of from 0.3:1 to 4:1.5. The ...

A Catalyst Composition for Different Reforming Techniques

The present invention provides a catalyst composition comprising different metal oxides wherein the catalyst composition comprising Ce, Cr and Ni oxides and a process for preparation thereof. The catalyst composition is used for different reforming techniques for the production of syn gas (CO+H) at the same time this material can be used in fuel cell as a anode for power generation as this synthesized material is having good thermal stability and can sustain various redox reaction cycles also. 1. A catalyst composition comprising of different metal oxides wherein the catalyst composition comprising Ce , Cr and Ni oxides.2. The catalyst as claimed in claim 1 , wherein said composition comprising Ce claim 1 , Cr and Ni oxides present in the ratio 1-50% w/w claim 1 , 20-49% w/w and 1-60% w/w respectively.3. The catalyst as claimed in claim 1 , wherein said catalyst is recyclable and stable upto 800° C. even after sintering at 1400° C.4. The catalyst as claimed in claim 1 , wherein said catalyst is supported or unsupported.5. The catalyst as claimed in claim 1 , wherein said catalyst is useful for oxidative steam reforming claim 1 , dry and tri reforming claim 1 , wherein said oxidative reforming is without of a need of a heat source.6. The catalyst as claimed in claim 1 , wherein said catalyst is useful for the production of syn gas and useful for internal as well as external reforming.7. A process for the preparation of a catalyst composition comprising of different metal oxides wherein the catalyst composition comprising Ce claim 1 , Cr and Ni oxides comprising the steps of:a. dissolving a nitrate precursor of metal in a solvent to obtain a solution of a metal nitrate precursor;b. dissolving citric acid in the solvent to obtain a solution of citric acid;c. adding the solution of metal nitrate precursor into the solution of citric acid followed by heating at temperature ranging from 100° C. to 190° C. until evaporation of solvent to form a gel; andd. keeping the gel ...

Water-Gas Shift Catalyst

A sintered pelletized catalyst precursor comprising iron oxides, including haematite, and CrOand optionally one or more of AlO, ZnO, MnO, MgO, and/or CuO, the pelletized catalyst precursor having an iron oxide content of 60 wt % to 95 wt %, when expressed as FeO, and a Cr(VI) content of less than 0.1 wt %, is physically stable on ignition or when subjected to a reducing gas sufficient to reduce the haematite to magnetite. 1. A pelletized catalyst precursor in the form of a sintered pellet comprising iron oxides , including haematite , and CrOand optionally one or more of AlO , ZnO , MnO , MgO , and/or CuO , the pelletized catalyst precursor having an iron oxide content of 60 wt % to 95 wt % , when expressed as FeO , and a Cr(VI) content of less than 0.1 wt % , both relative to the total weight of the pelletized catalyst precursor and wherein the pelletized catalyst precursor (a) exhibits a loss on ignition of less than 3 wt % and/or (b) when subjected to a step comprising subjecting the pelletized catalyst precursor to a reducing gas sufficient to reduce the haematite to magnetite , exhibits a volume shrinkage of less than 1.5% vol and/or retains at least 40% of its mean horizontal crush strength (MHCS).2. The pelletized catalyst precursor of claim 1 , wherein the CrOor the one or more optional AlO claim 1 , ZnO claim 1 , MnO claim 1 , MgO claim 1 , or CuO are present in a range of from 1 wt % to 10 wt % relative to the total weight of the pelletized catalyst precursor.3. The pelletized catalyst precursor of that contains CuO in a range of from 1 wt % to 10 wt % relative to the total weight of the pelletized catalyst precursor.4. The pelletized catalyst precursor of that has been pelletized with a pelleting aid or lubricant.5. The pelletized catalyst precursor of wherein essentially all of the iron oxides are present as haematite.6. The pelletized catalyst precursor of comprising acicular haematite.7. The pelletized catalyst precursor of that exhibits a mean ...

PROCESSES TO CREATE MULTIPLE VALUE STREAMS FROM BIOMASS SOURCES

Use of diverse biomass feedstock in a process for the recovery of target C5 and C6 alditols and target glycols via staged hydrogenation and hydrogenolysis processes is disclosed. Particular alditols of interest include, but are not limited to, xylitol and sorbitol. Various embodiments of the present invention synergistically improve overall recovery of target alditols and/or glycols from a mixed C5/C6 sugar stream without needlessly driving total recovery of the individual target alditols and/or glycols. The result is a highly efficient, low complexity process having enhanced production flexibility, reduced waste and greater overall yield than conventional processes directed to alditol or glycol production. 1. A process , comprising:providing a mixed C5/C6 monomer sugar stream derived from a plant biomass;selecting a target alditol or a target blend of alditols,hydrogenating continuously the mixed C5/C6 monomer sugar stream to form a mixed C5/C6 alditol stream;isolating the target alditol or target blend of alditols from the mixed C5/C6 alditol stream to leave a residual mixed C5/C6 alditol stream, wherein the isolating the target alditol or target blend of alditols comprises crystallization, chromatography, or crystallization and chromatography;continuous hydrogenolysis of the residual mixed C5/C6 alditol stream to form a mixed C2-C4 glycol stream; andisolating a target glycol or target blend of glycols from the mixed C2-C4 glycol stream;wherein at least 10% of the overall target product yield is either target alditol/target blend of alditols or target glycol/target blend of glycols.2. The process of claim 1 , wherein the mixed C5/C6 monomer sugar stream comprises greater than or equal to 60% of a C5 monomer sugar based on a combined total of C5 and C6 monomer sugars; orwherein the mixed C5/C6 monomer sugar stream comprises greater than or equal to 60% of a C6 monomer sugar based on a combined total of C5 and C6 monomer sugars.3. The process of claim 1 , further ...

SUPPORTED INTERMETALLIC COMPOUNDS AND USE AS CATALYST

A composition comprising a ternary intermetallic compound XYZ, wherein X, Y, and Z are different from one another; X being selected from the group consisting of Mn, Fe, Co, Ni, Cu, and Pd; Y being selected from the group consisting of Cr, Co, and Ni; and Z being selected from the group consisting of Al, Si, Ga, Ge, In, Sn, Zn, and Sb; wherein the ternary intermetallic compound is supported on a porous oxidic support material. The composition may be prepared by providing a liquid mixture of sources of X, Y, and Z, and the porous oxidic support material, removing the liquid and heating the resulting mixture in a reducing atmosphere. The composition is useful as catalyst. 1: A composition comprising a ternary intermetallic compound XYZ , whereinX, Y, and Z are different from one another;X being selected from the group consisting of Mn, Fe, Co, Ni, Cu, and Pd;Y being selected from the group consisting of Cr, Co, and Ni; andZ being selected from the group consisting of Al, Si, Ga, Ge, In, Sn, Zn, and Sb;wherein the ternary intermetallic compound is supported on a porous oxidic support material.2: The composition of claim 1 , wherein the porous oxidic support material comprises one or more selected from the group consisting of:silica,alumina,titania,zirconia, anda mixed oxide of one or more selected from the group consisting of Si, Al, Ti, and Zr.3: The composition of claim 1 , wherein X or Y is Co claim 1 , and wherein Z is selected from the group consisting of Al claim 1 , Ga claim 1 , In claim 1 , and Zn.4: The composition of claim 1 , wherein the porous oxidic support material comprises a mixed oxide of Si and Al.5: The composition of claim 1 , wherein in the composition claim 1 , the weight ratio of the ternary intermetallic compound relative to the porous oxidic compound is in the range of from 0.5:99.5 to 30:70.6: The composition of claim 1 , wherein Y is Ni claim 1 , and wherein Z is Al claim 1 , Si claim 1 , Ga claim 1 , In claim 1 , Sn claim 1 , or Sb.7: The ...

METHOD FOR OXIDIZING AMMONIA AND SYSTEM SUITABLE THEREFOR

A system suitable for oxidizing ammonia with oxygen in the presence of catalysts is described. The system includes a reactor equipped with at least one supply line for a reactant gas mixture and at least one discharge line for a process gas; a catalyst comprising at least one transition metal oxide that is not an oxide of a platinum metal; and a device for adjusting a molar ratio of oxygen to ammonia of less than or equal to 1.75 mol/mol in the reactant gas mixture by mixing an oxygen-containing gas stream having an Ocontent of <20% by volume with a chosen amount of ammonia. The oxygen-containing gas stream is produced by a device for: diluting an air stream with a gas stream comprising less than 20% by volume oxygen; or depleting oxygen from an oxygen-containing gas mixture, preferably from air; or by a combination thereof. 1. A system for oxidizing ammonia , comprising:A) a reactor for ammonia oxidation, equipped with at least one supply line for a reactant gas mixture and with at least one discharge line for a process gas;B) a catalyst arrangement inside the reactor, the catalyst comprising at least one transition metal oxide that is not an oxide of a platinum metal; and{'sub': '2', 'claim-text': c1) by a device for diluting an air stream with a gas stream that comprises less than 20% by volume oxygen; or', 'c2) by a device for depleting oxygen from an oxygen-containing gas mixture, preferably from air; or', 'c3) by a combination of measures c1 and c2., 'C) a device for adjusting a molar ratio of oxygen to ammonia in the reactant gas mixture of less than or equal to 1.75 mol/mol by mixing an oxygen-containing gas stream having an Ocontent of <20% by volume with a chosen amount of ammonia, wherein the oxygen-containing gas stream is produced2. The system as claimed in claim 1 , further comprising:D) a device for adjusting an outlet temperature of a product gas from the reactor based on a concentration of ammonia of the reactant gas mixture at an inlet of the ...

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

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

Methods of preparing a polymerization catalyst

A method of preparing a catalyst comprising contacting a support with a trivalent titanium compound and a chromium-containing compound. A catalyst composition comprising a support, chromium, and titanium, wherein the titanium is derived from TiCl 3 , Ti 2 (SO 4 ) 3 , Ti(OAc) 3 , Ti(+3) oxylate, Ti(NO 3 ) 3 , Ti(+3) lactate or combinations thereof.

Methods of preparing a polymerization catalyst

The invention relates to an olefin polymerization method comprising: using a catalyst which has been prepared by a method which comprises contacting a support with a chromium-containing compound and an aqueous solution comprising a trivalent titanium compound. In a further aspect the invention relates to a polymer produced by a catalyst; wherein the catalyst is produced by a method which comprises contacting a support with a chromium-containing compound and an aqueous solution comprising a trivalent titanium compound; wherein the catalyst, when contacted with an olefin monomer under suitable polymerization conditions, is effective to produce a polymer having an increased high load melt index, a lower molecular weight, a broader molecular weight distribution, or an increased melt index when compared to a polymer produced using an otherwise similar catalyst prepared with a tetravalent titanium species in aqueous solution.

Methods of preparing a polymerization catalyst

A method of preparing a catalyst comprising contacting a support with a trivalent titanium compound and a chromium-containing compound. A catalyst composition comprising a support, chromium, and titanium, wherein the titanium is derived from TiCl 3 , Ti 2 (SO 4 ) 3 , Ti(OAc) 3 , Ti(+3) oxylate, Ti(NO 3 ) 3 , Ti(+3) lactate or combinations thereof.