НАНЕСЕННЫЙ НА ДИОКСИД КРЕМНИЯ КАТАЛИЗАТОР

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

КАТАЛИЗАТОР ДЛЯ ОКИСЛЕНИЯ УГЛЕВОДОРОДОВ ПРИ ГАЗОФАЗНОМ КОНТАКТЕ, СПОСОБ ПОЛУЧЕНИЯ ЭТОГО КАТАЛИЗАТОРА И СПОСОБ ГАЗОФАЗНОГО ОКИСЛЕНИЯ УГЛЕВОДОРОДОВ С ИСПОЛЬЗОВАНИЕМ ЭТОГО КАТАЛИЗАТОРА

FIELD: chemistry. SUBSTANCE: invention relates to hydrocarbon oxidation catalysts. Described is a catalyst for oxidising hydrocarbons during gas-phase contact, containing a mixed oxide of molybdenum (Mo), vanadium (V), tellurium (Te) and niobium (Nb), having chemical formula 1: Mo 1.0 V a Te b Nb c o n , (l) where a, b or c independently denotes atomic molar ratios of vanadium, tellurium or niobium, provided that 0.01≤a≤1, 0.01≤b≤1, 0.01≤c≤1 and n denotes the atomic molar ratio of oxygen, which is determined by valence and atomic molar ratios of vanadium, tellurium and niobium, and tungsten (W) or tungsten oxide bonded to the mixed metal oxide, where the atomic molar ratio of tungsten bonded to the mixed metal oxide and molybdenum contained in the mixed metal oxide ranges from 0.00001:1 to 0.02:1. Described is a method of producing said catalyst involving steps for: preparing a first mixture of molybdenum (Mo) precursor, a vanadium (V) precursor, a tellurium precursor (Te), a niobium precursor (Nb) and acid; obtaining a mixed oxide of molybdenum (Mo), vanadium (V), tellurium (Te) and niobium (Nb) by calcining the first mixture; preparing a second mixture of mixed metal oxide and the tungsten precursor and calcining the second mixture. Described is a method for gas-phase oxidation of hydrocarbons, involving oxidation of hydrocarbons in the presence of the catalyst described above. EFFECT: high activity and selectivity of the catalyst. 10 cl, 2 tbl, 12 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 455 064 (13) C1 (51) МПК ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ B01J B01J B01J B01J C07C C07C C07C 23/00 37/04 37/08 23/44 51/16 51/21 253/24 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2010150512/04, 09.06.2009 (24) Дата начала отсчета срока действия патента: 09.06.2009 (73) Патентообладатель(и): ЭлДжи Кем, Лтд. (KR), ЭсЭнЮ Ар энд ДиБи Фаундейшн (KR) R U Приоритет(ы): (30) Конвенционный ...

СПОСОБ И РЕАКТОР ДЛЯ ПРИГОТОВЛЕНИЯ МЕТАНОЛА

... 1. Способ получения метанола, отличающийся тем, что указанный способ включает ! создание разности потенциалов между катодом (11) и анодом (12) в реакторе типа топливного элемента, ! проведение в реакторе первой операции (1), включающей первую требуемую катодную реакцию (a) между диоксидом углерода и водой ! ! с использованием катализатора, действие которого оптимизировано для проведения указанной реакции (a); ! транспортировку продуктов реакции, получаемых в первой операции (1), для проведения второй операции (2), и проведение второй требуемой катодной реакции (b) ! ! с использованием катализатора, действие которого оптимизировано для проведения указанной реакции (b), и ! транспортировку продуктов реакции, получаемых во второй операции (2), для проведения третьей операции (3), и проведение третьей требуемой катодной реакции (c) ! ! с использованием катализатора, действие которого оптимизировано для проведения указанной реакции (c). ! 2. Способ по п.1, отличающийся применением катализатора ...

МОЛИБДЕНСОДЕРЖАЩИЙ КАТАЛИЗАТОР, СПОСОБ ЕГО ПОЛУЧЕНИЯ И СПОСОБ ПОЛУЧЕНИЯ МЕТИЛМЕРКАПТАНА

... 1. Катализатор на носителе, включающий ! а) соединение молибдена и калия в качестве активных компонентов, причем молибден и калий могут представлять собой составляющие одного соединения; ! б) промотор, включающий ТеO2, и ! в) оксидный носитель. ! 2. Катализатор в соответствии с п.1, в котором массовые соотношения компонентов следующие: ! ТеO2/KMoO4/носитель=(1-20)/(1-50)/100 или ! TeO2/MoO3/K2O/носитель=(1-20)/(1-50)/(1-50)/100. ! 3. Катализатор в соответствии с п.2, в котором массовые соотношения компонентов следующие: ! (1) TeO2/KMoO4/носитель=(3-12)/(15-30)/100 или ! (2) TeO2/MoO3/K2O/носитель=(3-12)/(15-30)/(8-20)/100. ! 4. Катализатор в соответствии с п.1, в котором носитель выбирают из группы, включающей SiO2, Al2O3, TiO2, Al2O3-SiO2, ZrO2, цеолиты, содержащие углерод материалы или смеси перечисленных веществ. ! 5. Катализатор в соответствии с п.1, который содержит активный центр состава Mo-O-K. !6. Катализатор в соответствии с п.п.1-5, сульфидированный путем воздействия атмосферы ...

ОКИСЛИТЕЛЬНОЕ ДЕГИДРИРОВАНИЕ АЛКАНОВ (ОД)

СПОСОБ ПРОИЗВОДСТВА НЕНАСЫЩЕННОГО НИТРИЛА

... 1. Способ производства ненасыщенного нитрила с помощью реакции аммоксидирования пропана в паровой фазе с применением реактора с кипящим слоем в присутствии сложнооксидного катализатора, содержащего Mo, V и Nb, при этом способ содержит стадию:добавления в реактор с кипящим слоем соединения вольфрама с регулированием молярного отношения (отношение W/Mo) вольфрама, содержащегося в соединении вольфрама, к молибдену, содержащемуся в сложнооксидном катализаторе, который находится в реакторе с кипящим слоем, таким образом, чтобы молярное отношение находилось в диапазоне от 0,0001 до 0,1.2. Способ производства ненасыщенного нитрила по п. 1, содержащий стадию добавления в реактор с кипящим слоем соединения молибдена.3. Способ производства ненасыщенного нитрила по п. 1 или 2, в котором сложнооксидный катализатор содержит сложный оксид с составом, представленным следующей формулой (1):MoVNbAXZO(1),в которой компонент A представляет собой, по меньшей мере, один или несколько элементов, выбранных из ...

Способ получения метакрилонитрила

Способ получения акрилонитрила

Production of acrolein or acrylic acid involves absorption of propane and propene from a gas mixture followed by desorption and oxidation, with no catalytic dehydrogenation of propane and no added oxygen

Acrolein and acrylic acid are produced from propane and propene by absorption/desorption of propane and propene from a gas mixture followed by oxidation, in which no heterogeneously catalyzed dehydrogenation of propane occurs between the desorption and oxidation stages without addition of oxygen. Acrolein and acrylic acid are produced from propane and propene by: (a) separation of propane and propene from a gas mixture (A) by absorption in an absorption medium; (b) separation of propane and propene from the absorbent to give a mixture (B) containing propane and propene; and (c) using mixture (B) for oxidation to the required product(s). In this process, no catalytic dehydrogenation of propane without the addition of oxygen is carried out between stages (b) and (c).

Katalysatorzusammensetzung und ihre Verwendung zur Herstellung ungesaettigter Nitrile und zur Oxidation von Olefinen

Kathodenkatalysator für eine Brennstoffzelle, Membran-Elektroden Einheit und Brennstoffzelle mit einer solchen Einheit

A method for preparing acrylonitrile

Acrylonitrile is prepared by passing a gaseous mixture of propylene, ammonia and oxygen or air at elevated temperature over a catalyst consisting of tellurium oxide and either a salt of phosphomolybdic acid or molybdenum oxide, supported on alumina previously activated by heating at 300 DEG to 1000 DEG C. The gas mixture is passed over the catalyst at 300 DEG to 480 DEG C.ALSO:A catalyst for preparing acrylonitrile consists of tellurium oxide and either a salt of phosphomolybdic acid or molybdenum oxide, supported on alumina previously activated by heating at 300-1000 DEG C. The activated alumina is mixed with the other materials, moulded, and heated e.g. at above 300 DEG C. The materials may be in such proportions that the molar ratii are P = 0 to 3, Te = 3 to 15, Mo = 5 to 20 and Al2O3= 20 to 50. In an example a catalyst is prepared from alumina previously activated by heating at 300-1000 DEG C., tellurium oxide and ammonium phosphomolybdate. Comparative examples describe the use of SiO2 ...

Production of styrenes and of oxirane compounds

... 1,133,313. Coproduction of epoxides and styrenes. HALCON INTERNATIONAL Inc. 24 Nov., 1965 [30 Nov., 1964], No. 49907/65. Addition to 1,097,132. Heading C2C. [Also in Division C5] In a process for the co-production of an epoxide and a styrene, an alpha-aralkyl hydroperoxide, having at least one hydrogen atom attached to a carbon atom adjacent to the carbon atom of the hydroperoxy group, is reacted in the liquid phase with a C 2-30 olefinically unsaturated compound, which has a different carbon skeleton from that of the hydroperoxide, in the presence of a Ti, Ta, Se, Te, Nb, Cr, Zn, U or Re catalyst to produce an epoxide and an alpha-aralkyl alcohol corresponding to the hydroperoxide and said alcohol is separated and dehydrated to the corresponding alcohol. The aralkyl hydroperoxides may be obtained by oxidation of the appropriate aralkanes, e.g. cumene and ethylbenzene. Epoxidation may be effected at - 20‹ to 200‹ C. in the presence of an inert solvent using a catalyst which is soluble in ...

PROCESS FOR IMPROVING ACTIVITY OF TELLURIUM CONTAINING METAL OXIDE CATALYSTS

A regeneration process for tellurium-containing metal oxide catalysts used in the process for oxidation, ammoxidation or oxidative dehydrogenation of organic compounds at a temperature of about 300 DEG C. to about 600 DEG C. The process can be effectively applied to such catalysts which have become partially deactivated during the reaction. According to the present process, the deactivated catalyst is regenerated at the reaction temperature under a non-reductive atompshere by contacting the deactivated catalyst with a tellurium-enriched metal oxide catalyst having a tellurium content higher than that of a fresh metal oxide catalyst used in the reaction, or by contacting the deactivated catalyst at the reaction temperature with a tellurium-molybdenum-enriched catalyst system selected from the group consisting of (i) a physical blend of a tellurium-enriched catalyst and a molybdenum-enriched catalyst and (ii) a tellurium-molybdenum-enriched catalyst, the tellurium and molybdenum contents ...

PROCESS FOR IMPROVING ACTIVITY OF TELLURIUM CONTAINING METAL OXIDE CATALYSTS

Improvements in the manufacture and production of unsaturated hydrocarbons of low boiling point

... 322,284. Johnson, J. Y., (I. G. Farbenindustrie Akt.-Ges.). Oct. 11, 1928. Liquid fuels; mineral oils.-Low boiling and unsaturated hydrocarbons obtained by treating mixtures of oxides of carbon and hydrogen at an elevated temperature and under any desired pressure with catalysts which contain besides metals of the eighth group of the periodic system, alkali metal compounds and small quantities of sulphur, selenium or tellurium in a free or combined state, are used as anti-knock benzines, as additions to other benzines to prevent knocking, and for the manufacture of lubricating and insulating oils by condensation by means of aluminium chloride, boron fluoride and the like. Specification 312,717, [Class 1 (i), Chemical processes &c.], is referred to in the Provisional Specification.

PREPARATION OF STABLE TELLURIUM-CONTAINING SOLUTION FROM METALLIC TELLURIUM AND PROCESS FOR PRODUCING TELLURIUM-ANTIMONY CONTAINING OXIDE CATALYST USING SAID SOLUTION

CATALYTIC COMPOSITIONS SUITABLE FOR USE IN THE AMMOXIDATION OXIDATION AND OXIDATIVE DEHYDROGENATION OF OLEFINS AND PROCESSES FOR THE PREPARATION AND USES OF SUCH COMPOSITIONS

... 1408800 Oxidation/ammoxidation catalyst SNAMPROGETTI SpA 27 Feb 1973 [1 March 1972] 9643/73 Heading B1E [Also in Division C2 and C5] An oxidation or ammoxidation catalyst composition comprises a mixture of the oxides of tellurium and titainium, wherein the atomic ratio Ee/Ti is from 10:1 to 1:5 and wherein the composition is free from molybdenum and vanadium. The composition may also contain an element of Gp V, e.g. phosphorus. The composition may be formed by reacting tellurium, telluric acid or tellerium oxide with titanium dioxide or titanium chloride and, optionally, phosphoric acid.

Production of Acrylic Acid

... 1,193,489. Making acrylic acid. BADISCHE ANALIN- & SODA-FABRIK A.G. 27 Oct., 1967 [28 Oct., 1966], No. 48858/67. Heading C2C. Propylene or acrolein is oxidized to acrylic acid in the presence of molecular oxygen and a catalyst which has been made by mixing in the solid state CoO or a precursor therefor, MoO 3 or a precursor therefor and heating at 300-800‹ C. Example 6 describes the oxidation at 356- 390‹ C. using a Co, Mo, Te catalyst.

The Preparation of Aromatic Nitriles

... 1,160,737. Aminoxidation catalysts. MONTECATINI EDISON S.p.A. 14 Sept., 1966 [22 Sept., 1965], No. 41788/66. Heading B1E. [Also in Divisions Cl and C2] Heteropolycompounds of the formulae Mx (Cey Mo 12 O w ) and Mx (Cey Mo 10 V 2 O w ) in which M represents a bismuth or tellurium atom, x is from 1 to 10, y is from 1 to 8 and w is from 38 to 82 are deposited on a carrier by impregnation of the carrier, e.g. silica gel or an aerogel, with a solution of the compound or by mixing the solution with a silica sol and drying the mixture. The deposited compound is made catalytically active by heating at 400-600‹C for 5-20 hours and is used in a fluidised or fixed bed to prepare aromatic nitriles from alkyl-sulbsitituted aromatic hydrocarbon, ammonia and oxygen.

PROCESS FOR THE VAPOUR-PHASE OXIDATION OF LOWER OLEFINS

... 1,247,386. Oxidation catalysts. TOA GOSEI CHEMICAL INDUSTRY CO. Ltd. 9 Sept., 1968 [19 Dec., 1967], No. 42852/68. Heading B1E. [Also in Division C2] A catalyst comprising chromium, molybdenum and tellurium in relative proportions such that the atom percentages of chromium, molybdenum and tellurium, calculated as percentages of the total number of atoms of chromium, molybdenum and tellurium present in the catalyst, are 5 to 39, 51 to 94.5 and 0.5 to 10, respectively, is prepared by a process which comprises either preparing a mixed aqueous solution containing a compound of trivalent chromium, molybdic acid or a salt thereof and telluric acid or a salt thereof, drying the solution to form a deposit and calcining the deposit or preparing a mixed aqueous solution containing a compound, of trivalent chromium and molybdic acid or a salt thereof, drying the solution to form a deposit, impregnating the deposit with a solution of telluric acid or a salt thereof and calcining the impregnated deposit ...

CATALYST FOR PARTIAL HYDROGENATION OF ACETYLENIC COMPOUND

... 1504187 Hydrogenation catalyst BASF AG 2 July 1975 [3 July 1974] 27815/75 Heading B1E [Also in Division C2C] A catalyst for the selective hydrogenation of acetylenic compounds to olefinic compounds comprises a support and an active component comprising palladium and either (i) zinc plus bismuth and/or tellurium, (ii) cadmium plus bismuth and/or tellurium, or (iii) cadmium plus zinc, optionally plus bismuth and/or tellurium. The active component may comprise 20-70pbw of Pd, 10-30pbw of Zn and/or Cd and 10-30pbw of Bi and/or Te. The support may be alumina or pumice, e.g. gamma-alumina or Italian pumice. The catalyst may be in the form of particles of average diameter 0.05-0.35mm.

Catalyst improved for the hydrocarbon oxidation.

PROCEDURE FOR THE PRODUCTION OF AN OXIDATION OF CATALYST

PROCEDURE FOR THE PRODUCTION OF ACRYLIC ACID OR METHACRYLSAEURE

PROCEDURE FOR THE PRODUCTION OF A METALLIC OXIDE CATALYST

VERFAHREN ZUR HERSTELLUNG VON BUTENDIOLDIACETATEN

VERFAHREN ZUR HERSTELLUNG EINES OXYDATIONS- KATALYSATORS

PROCEDURE FOR THE PRODUCTION OF AN INSATIATED CARBONIC ACID FROM AN ALKANE

PROCEDURE FOR THE PRODUCTION OF UNGESATTIGTEN NITRILES

PROCEDURE FOR THE PRODUCTION OF ALKYL STAR OF INSATIATED SAEUREN

PROCEDURE FOR THE PRODUCTION OF ACRYLONITRILE OR METHACRYLNITRIL

PROCEDURE FOR THE PRODUCTION OF ANTIMONY ABSTENTION METALLIC OXIDE CATALYSTS.

PROCEDURE FOR THE PRODUCTION OF METHACRYLNITRIL

CATALYST FOR THE PRODUCTION OF ACETIC ACID OR ACETIC ACID AND ETHYL ACETATE, PROCEDURE FOR ITS PRODUCTION AND PROCEDURE FOR THE PRODUCTION OF ACETIC ACID OR ACETIC ACID AND ETHYL ACETATE USING THE SAME

PROCEDURE FOR THE PRODUCTION OF BUTENDIOLDIACETATEN

Procedure for the oxidation from Olefinen to insatiated aldehydes

CATALYSTS FOR AMMOXIDATION OF OLEFINES

PROCESS FOR THE PRODUCTION OF ANTIMONY-CONTAINING METAL OXIDE CATALYSTS

ODH CATALYST FORMULATIONS

The oxidative dehydrogenation of ethane comprises contacting a mixture of ethane and oxygen in an ODH reactor with an ODH catalyst under conditions that promote oxidation of ethane into ethylene. Conditions within the reactor are controlled by the operator and include, but are not limited to, parameters such as 5 temperature, pressure, and flow rate. Conditions will vary and can be optimized for a specific catalyst, or whether an inert diluent is used in the mixing of the reactants. Disclosed herein is a catalyst consisting of: Mo0-1W0.3-1V0.2-0.4Te0.06-0.10Fe0.0-0.10Nb0.08-0.18Ox where X is determined by the valance of the metals.

PROCESS FOR THE OXIDATION OF OLEFINS

PROCESS FOR THE OXIDATION OF OLEFINS USING CATALYSTS CONTAINING VARIOUS PROMOTER ELEMENTS Iron-bismuth-molybdate catalysts further containing specific promoter elements have been found to exhibit excellent redox stability even under high stress conditions in the catalytic oxidation of olefins to unsaturated aldehydes and acids.

PROCESS FOR PRODUCING ACRYLONITRILE

A process for producing acrylonitrile by the vapor-phase catalytic ammoxidation of propylene, which comprises (I) reacting propylene, a molecular oxygen-containing gas and ammonia in the presence of a catalyst expressed by the following empirical formula FeaSbbMocMedTeeOfNagOh.(SiO)i wherein Me is at least one element selected from the group containing of V and W, C is at least one element selected from the group consisting of Cu, Mg, In and Ni, and the subscripts a, b, c, d, e, f, g, h and i each represents atomic rations such that when a-10; b-13 to 28; c-0.1 to 2.5; d-0.05 to 1; e-0.2 to 5; f-0 to 4(in which case b-13 to 20), or f-2 to 6 (in which case b-20 to 28); g-0 to 3; h-the number of oxygens corresponding to the oxide formed by the combination of the components, and i-25 to 200; in a fluidized bed catalytic reaction zone at a temperature of about 380 to about 500.degree.C and a pressure of about 0.2 to about 3 kg/cm2-G while adjusting the propylene/oxygen/ammonia molar ratio to ...

MANUFACTURE OF MALEIC ANHYDRIDE FROM BUTANE

CATALYTIC REMOVAL OF SULPHUR-CONTAINING COMPOUNDS FROM FLUID STREAMS BY DECOMPOSITION

This invention provides a catalyst and method for removing sulphur compounds from a fluid stream and decomposing such compounds to produce sulphur. Sour natural gas can be sweetened effectivey by this invention, and sulfur can be prepared thereby. The invention employs a catalyst containing an alkali metal sulfide and sulfides(s) or selenide(s) of metal(s) showing polyvalent and/or amphoteric character, e.g. Zn, etc. The catalyst is generally impregnated on a microporous type support (e.g., alumina) and is capable of providing reactive oxygen. Its activity is sustained by exposure to small amounts of oxygen either while decomposing the sulphur compound, or thereafter.

PRODUCTION OF ANTHRAQUINONE

PROCESS FOR THE PRODUCTION OF UNSATURATED NITRILES

PROCESS FOR PREPARING METHACROLEIN FROM ISOBUTENE AND OXYGEN

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

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

CATALYST FOR CONVERSION OF PROPYLENE TO PRODUCT COMPRISING A CARBOXYLIC ACID MOIETY

In accordance with the invention, there is provided a novel catalyst composition comprising MoVGaPdNbXY, wherein X comprises La, Te, Ge, Zn, In, or W; and Y comprises Al or Si; wherein Mo, V, Ga, Pd, Nb, La, Te, Ge, Zn, In, W, Al, or Si are optionally present in combination with oxygen; wherein the catalyst does not comprise an additional element that acts as a catalyst in the conversion of a propylene to the product. Also, disclosed is a method for the conversion of a propylene to a carboxylic acid moiety by contacting the propylene with the disclosed catalyst.

AGGLOMERATED ODH CATALYST

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

ALKANE OXIDATIVE DEHYDROGENATION AND/OR ALKENE OXIDATION

The invention relates to a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms, comprising contacting a first gas stream comprising oxygen and the alkane containing 2 to 6 carbon atoms and/or the alkene containing 2 to 6 carbon atoms with a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium; followed by contacting a second gas stream comprising methane, an inert gas or oxygen or any combination of two or more of these with the catalyst, wherein the second gas stream comprises 0 to 25 vol.% of the alkane containing 2 to 6 carbon atoms and/or alkene containing 2 to 6 carbon atoms.

Procédé de préparation simultanée d'époxydes et d'alcools aralcoyliques

Procédé de préparation d'aldéhydes et d'acides carboxyliques non saturés à partir de monooléfines et catalyseur pour la mise en oeuvre du procédé

Verfahren zur Herstellung von Allylchlorid und seinen Monomethylsubstitutionsprodukten

Verfahren zur Herstellung von Allylchlorid und seinen Monomethylsubstitutionsprodukten

Verfahren zur katalytischen Herstellung aromatischer Nitrile

Katalysator zur Oxydation von Olefinen zu entsprechenden ungesättigten Säuren

Procédé pour isoler un oxirane d'un mélange d'époxydation

Procédé de préparation d'oxiranes

Verfahren zur Herstellung von ungesättigten Nitrilen

Procédé de préparation d'acrylonitrile

Procédé de fabrication de nitriles insaturés

Procédé amélioré de fabrication catalytique de nitriles insaturés

VERFAHREN ZUR HERSTELLUNG VON ANTHRACHINON.

Procédé de préparation d'oxiranes

Verfahren zur Gewinnung ungesättigter Nitrile

Verfahren zur Herstellung von ungesättigten Nitrilen

Verfahren zur Herstellung von 1,2-Dichloräthan

Verfahren zur Herstellung von 1-Cyan-1,3-butadien

Procédé pour l'oxydation d'oléfines

Procédé pour la production simultanée d'un styrène et d'un époxyde

Procédé de fabrication de nitriles insaturés utilisant une composition catalytique

PROCEDURE FOR THE PRODUCTION OF ALPHA, BETA-INSATIATED ALDEHYDES FROM OLEFINEN AND CATALYST.

Oxidation catalyst.

Process for the preparation of maleic anhydride

Maleic anhydride is prepared by a novel 2-step process. In the first step, butadiene is prepared from n-butane or n-butene or from a mixture of these and molecular oxygen in an undivided reaction zone of a tubular reactor. This process is carried out in the presence of a catalyst. In the second step, which is carried out in the downstream zone of the tubular reactor, maleic anhydride is obtained from the product of the first step, which may still contain starting materials besides the butadiene, and in the presence of a second catalyst.

PROCEDURE FOR THE PRODUCTION OF ESTERS OF INSATIATED SAEUREN.

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА С КРЕМНЕЗЕМНЫМ НОСИТЕЛЕМ И СПОСОБ ПРОИЗВОДСТВА НЕНАСЫЩЕННОЙ КАРБОНОВОЙ КИСЛОТЫ ИЛИ НЕНАСЫЩЕННОГО НИТРИЛА

Настоящее изобретение относится к получению катализатора, нанесенного на кремнезем, обладающего превосходным выходом целевого продукта и превосходной стойкостью катализатора к истиранию. Способ получения катализатора, нанесенного на кремнезем, включающий в себя Мо, V, Nb и компонент Х (Sb и/или Те), используемого в парофазном каталитическом окислении или аммоксидировании пропана, включающий стадии: (I) приготовления раствора сырьевой смеси путем смешивания Мо, V, Nb, компонента X, золя кремниевой кислоты и воды; (II) получения сухого порошка путем высушивания раствора сырьевой смеси; и (III) получения катализатора, нанесенного на кремнезем, путем прокаливания сухого порошка, причем золь кремниевой кислоты содержит 10-270 мас.ч. на миллион нитрат-ионов, исходя из содержания SiO2.

catalyst of ammoxidation and method of obtaining acrylonitrile or metacrylonitrile

METHOD OF PREPARING CATALYST, CATALYST, AND METHOD FOR OXIDATIVE DEHYDROGENATION OF HYDROCARBONS

Preparation of chalcogenide semiconductor CdX compounded H-TiO2 based nanotube array

Method for producing silica-supported catalyst, and method for producing unsaturated carboxylic acid or unsaturated nitrile

Improved (amm)oxidation method for conversion of lower alkane

New catalytic and manufactoring process system of acids and unsaturated aldehydes

Semiconductor photocatalyst for the photocatalytic reforming of biomass derivatives for hydrogen generation, and preparation and use thereof

Disclosed are a semiconductor photocatalyst for the photocatalytic reforming of biomass derivatives for hydrogen generation, and preparation and use thereof. The semiconductor photocatalyst has the atomic composition ratio of M˜N-Ax; wherein M˜N are IIB group elements to VIA group elements, or IIIA group elements to VA group elements, A being one element or more than two elements selected from the group consisting of cobalt, nickel, iron, copper, chromium, palladium, platinum, ruthenium, rhodium, iridium and silver; and 0.02%≦x≦1.0%. The method of in-situ preparation of the highly effective semiconductor photocatalyst and catalytically reforming biomass derivatives for hydrogen generation by driving photoreaction with visible light via quantum dots is simple, fast, highly effective, inexpensive and practical. The in situ reaction can occur in sunlight without the need of harsh conditions such as calcination.

Process for producing olefin oxide

A process for producing an olefin oxide which comprises reacting an olefin with oxygen in the presence of a catalyst comprising a copper oxide and a tellurium oxide.

DIRECT CONVERSION OF OLEFIN TO OLEFIN OXIDE BY MOLECULAR OXYGEN

The present invention relates to a direct conversion of olefin to olefin oxide, which are important and versatile intermediates used in the production of a large variety of valuable consumer products such as polyurethane foams, polymers, alkylene glycol, cosmetics, food emulsifiers and as fumigants and insecticides. More specifically, the present invention provides a process for producing an olefin oxide which comprises reacting an olefin with oxygen in the presence of a halogen compound additive and a catalyst comprising copper, ruthenium or both thereof.

STEAM RE-CALCINATION OF MIXED METAL OXIDE CATALYSTS

A process for producing a catalyst for the (amm)oxidation of alkanes comprises calcination of a crystalline mixed metal oxide catalyst partially or wholly in the presence of steam. 2. The process of further comprising: (c) grinding the re-calcined mixed metal oxide catalyst.3. The process of wherein the water vapor comprises from 0.01 to 100 volume percent claim 1 , based on the total volume of gas in the atmosphere.4. The process of wherein the water vapor comprises from 0.5 to 10 volume percent claim 1 , based on the total volume of gas in the atmosphere.5. The process of wherein the water vapor comprises from 1 to 3.5 volume percent claim 1 , based on the total volume of gas in the atmosphere.6. The process of wherein Z is Pd.7. The process of wherein X is Te.8. The process of wherein calcining the first catalyst is done in 2 stages claim 1 , wherein claim 1 , in the first stage claim 1 , the first catalyst is calcined in an inert or oxidizing environment at a temperature of from 100° C. to 400° C. claim 1 , for from 15 minutes to 40 hours claim 1 , and in a second stage the material from the first stage is calcined in a non-oxidizing environment at a temperature of from 400° C. to 650° C. for 0.1 to 25 hours.9. A process for the (amm)oxidation of alkanes claim 1 , the process comprising (amm)oxidizing an alkane in the presence of a final catalyst of .10. The process of wherein the calcined MMO solid first catalyst has an X-ray diffraction pattern showing the orthorhombic phase as the major crystal phase with main peaks with 2θ at 6.7° claim 1 , 7.8° claim 1 , 22.1° claim 1 , and 27.2°12. The process of wherein Z is Pd and X is Te.13. The process of wherein Z is Pd and X is Te. This application claims priority from provisional application Ser. No. 61/467,418, filed Mar. 25, 2011, which is incorporated herein by reference in its entirety.The present invention relates to mixed metal oxide (amm)oxidation catalysts.Mixed metal oxide (MMO) catalysts are well known for ...

Isomerization of light alpha-olefins to light internal olefins

The present invention relates to a process for isomerizing linear alpha-olefins having from 4 to 8 carbon atoms over a heterogeneous catalyst, wherein the catalyst comprises a hydrogenation metal and a selectivity promoter selected from among selenium and tellurium on a support, and also a process for preparing 1-olefins by a metathesis reaction of 2-olefins with ethene, wherein the 2-olefins are prepared by the above mentioned isomerization process.

CONTROLLED PRESSURE HYDROTHERMAL TREATMENT OF ODH CATALYST

The preparation of an oxidative dehydrogenation catalyst comprising Mo, V, Nb and Te using a hydrothermal step the activity and reproducibility of the catalyst is improved by conduction the hydrothermal step at higher pressures while permitting gaseous products to leave the reactor. In some instances a condenser may be upstream of the pressure relief valve. 1. A process for synthesis of a catalyst for oxidative dehydrogenation of paraffins via a hydrothermal treatment comprising:i) preparing an aqueous slurry comprising Mo, V, Nb and Te salts in a molar ratio of metal elements 1:0.3 to 3; 0.05 to 0.25; and 0.08 to 0.2 at a temperature from 25° C. to 80° C.;ii) heating slurry in a reactor to a temperature from 80° to 220° C. at a pressure equal or above the saturated water vapor pressure at the corresponding reaction temperature, for a period of time not less than 1 hour with agitation and simultaneous removal of gaseous byproduct species produced during the reaction.iii) letting the reactor cool and depressurizing the reactor and recovering the catalyst as a solid.2. The process according to claim 1 , wherein the temperature of the reactor is from 150° C.-185° C.3. The process according to claim 2 , wherein the pressure in the reactor is from 10 psi to 190 psi (960 kPa to 1300 kPa).4. The process according to claim 1 , wherein there is a condenser upstream of a pressure control device.5. The process according to 4 claim 1 , wherein the condenser is operated at a temperature above 0° C. and below reaction temperature.6. The process according to claim 1 , wherein the gaseous species are removed by being vented from the reactor through the pressure control device.71. The process according claim 1 , wherein the gaseous species are removed from the reactor using one or more methods selected from gas absorption claim 1 , gas adsorption claim 1 , membrane separation claim 1 , and chemicals transformation.8. The process according to wherein the time of hydrothermal ...

PRODUCTION OF PRODUCTS FROM NATURAL RESOURCES

The method disclosed herein relates to two stage catalytic processes for converting syngas to acetic acid, acrylic acid and/or propylene. More specifically, the method described and claimed herein relate to a method of producing acrylic acid and acetic acid comprising the steps of: a) providing a feedstream comprising syngas; b) contacting the feedstream with a first catalyst to produce a first product stream comprising C-Colefins and/or C-Cparaffins; and c) contacting the first product stream with oxygen gas and a second catalyst, thereby producing a second product stream comprising acrylic acid and acetic acid, wherein there is no step for separating the components of the first product stream before the first product stream is contacted with the second catalyst. 1. A method of producing acrylic acid and acetic acid comprising the steps of:a) providing a feedstream comprising syngas;{'sub': 2', '3', '2', '3, 'b) a step consisting of contacting the feedstream with a first catalyst to produce a first product stream comprising C-Colefins and/or C-Cparaffins; and'}c) contacting the first product stream with oxygen gas and a second catalyst, thereby producing a second product stream comprising acrylic acid and acetic acid,wherein there is no step for separating the components of the first product stream before the first product stream is contacted with the second catalyst.2. The method of claim 1 , wherein the method further comprises separating the acetic acid and the acrylic acid.3. The method of claim 1 , wherein the first catalyst comprises a mixed metal oxide represented by the formula{'br': None, 'sub': a2', 'b2', 'z2', 'y2', 'd2', 'f2, 'CoMnLaPM2O,'}wherein a2 is 1;wherein b2 is from 0.8 to 1.2;wherein z2 is greater than 0 to 0.5;wherein y2 is greater than 0 to 0.5;wherein M2 comprises an alkali metal, alkaline earth metal, or transition metal, or a mixture thereof,wherein d2 is greater than 0 to 0.5; andwherein f2 is a number determined by the valence ...

CATALYST FOR ALKANE OXIDATIVE UU DEHYDROGENATION AND/OR ALKENE OXIDATION

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

CATALYST FOR ALKANE OXIDATIVE DEHYDROGENATION AND/OR ALKENE OXIDATION

The invention relates to a process for treating a catalyst for alkane oxidative dehydrogenation and/or alkene oxidation, which catalyst is a mixed metal oxide catalyst containing molybdenum, vanadium and niobium, wherein the process comprises: contacting, during a period of time from 30 minutes to shorter than 5 hours, the catalyst with a gas mixture comprising an inert gas and oxygen (O), wherein the amount of oxygen is of from to less than 10,000 parts per million by volume (ppmv), based on the total volume of the gas mixture, at an elevated temperature. 1. A process for treating a catalyst for alkane oxidative dehydrogenation and/or alkene oxidation , which catalyst is a mixed metal oxide catalyst containing molybdenum , vanadium and niobium , wherein the process comprises:{'sub': '2', 'contacting, during a period of time from 30 minutes to shorter than 5 hours, the catalyst with a gas mixture comprising an inert gas and oxygen (O), wherein the amount of oxygen is of from 1 to less than 10,000 parts per million by volume (ppmv), based on the total volume of the gas mixture, at an elevated temperature.'}2. A process according to claim 1 , wherein the temperature is of from 300 to 900° C.3. A process according to claim 1 , wherein the amount of oxygen is of from 10 to 7 claim 1 ,000 parts per million by volume.4. A process according to claim 1 , wherein the catalyst additionally contains tellurium.5. A process for preparing a catalyst for alkane oxidative dehydrogenation and/or alkene oxidation claim 1 , which catalyst is a mixed metal oxide catalyst containing molybdenum claim 1 , vanadium and niobium claim 1 , wherein the process comprises:a) preparing a catalyst containing molybdenum, vanadium and niobium;{'sub': '2', 'b) contacting the catalyst with oxygen (O) at an elevated temperature, to obtain a mixed metal oxide catalyst containing molybdenum, vanadium and niobium; and'}{'sub': '2', 'c) contacting, during a period of time from 30 minutes to shorter than 5 ...

AGGLOMERATED ODH CATALYST

Oxidative dehydrogenation catalysts for converting lower paraffins to alkenes such as ethane to ethylene when prepared as an agglomeration, for example extruded with supports chosen from slurries of TiO, ZrOAlO, AlO(OH) and mixtures thereof have a lower temperature at which 25% conversion is obtained. 1. An agglomerated catalyst comprising:from 10 to 95 weight % of a catalyst of the formula:{'sub': 1.0', '0.12-0.49', '0.6-0.16', '0.15-0.20', 'd', '2', '2', '2', '3', '2, 'MoVTeNbOwherein d is a number to satisfy the valence of the oxide; and from 5-90 weight % of a binder chosen from acidic, basic or neutral binder slurries of TiO, ZrOAlO, AlO(OH) and mixtures thereof provided that ZrOis not used in combination with an aluminum containing binder.'}2. The agglomerated catalyst according to claim 1 , having a cumulative surface area less than 35 m/g as measured by BET.3. The agglomerated catalyst according to claim 2 , having a cumulative pore volume from 0.05 to 0.50 cm/g.4. The agglomerated catalyst according to claim 2 , having a pore size distribution less than 4% having pore width size less than 150 Angstroms.5. The agglomerated catalyst according to claim 2 , having a percent pore area distribution less than 40% and corresponding percentage of pore volume less than 20%.6. The agglomerated catalyst according to in the shape of a sphere claim 2 , rod claim 2 , ring claim 2 , or a saddle having a size from about 1.3 mm to 5 mm.7. The agglomerated catalyst according to claim 6 , wherein the binder is an acidified binder.8. The agglomerated catalyst according to claim 6 , wherein the binder is a base treated binder.9. The agglomerated catalyst according to claim 7 , in the shape of rods having an aspect ratio from 1 to 5/1.3 having a crush strength up to 100 N/mm.10. The agglomerated catalyst according to claim 8 , in the shape of rods having an aspect ratio from 1 to 5/1.3 having a crush strength up to 100 N/mm.11. The agglomerated catalyst according to claim 7 , in ...

OXIDATIVE DEHYDROGENATION CATALYSTS

Provided in this disclosure are oxidative dehydrogenation catalysts that include a mixed metal oxide having the empirical formula: 1. An oxidative dehydrogenation catalyst comprising a mixed metal oxide having the empirical formula:{'br': None, 'sub': 1.0', '0.12-0.49', '0.05-0.17', '0.10-0.20', 'd, 'MoVTeNbO'} d is a number to satisfy the valence of the oxide, and', 'the oxidative dehydrogenation catalyst is characterized by having XRD diffraction peaks (2θ degrees) at 22±0.2, 27±0.2, 28.0±0.2, and 28.3±0.1., 'wherein2. The oxidative dehydrogenation catalyst of claim 1 , wherein the catalyst is prepared by a process comprising wet ball milling a pretreated oxidative dehydrogenation catalyst having the empirical formula:{'br': None, 'sub': 1.0', '0.12-0.49', '0.05-0.17', '0.10-0.20', 'd, 'MoVTeNbO'}wherein d is a number to satisfy the valence of the oxide.3. The oxidative dehydrogenation catalyst of claim 1 , wherein the aspect ratio of the peak at 27±0.2 to the peak at 22±0.2 is 0.55:1 to 0.65:1.4. The oxidative dehydrogenation catalyst of claim 1 , wherein the aspect ratio of the peak at 27±0.2 to the peak at 22±0.2 is about 0.60:1.5. The oxidative dehydrogenation catalyst of claim 1 , wherein the aspect ratio of the peak at 28.3±0.1 to the peak at 27±0.2 is 0.50:1 to 0.80:1.6. The oxidative dehydrogenation catalyst of claim 1 , wherein the aspect ratio of the peak at 28.3±0.1 to the peak at 27±0.2 is 0.60:1 to 0.70:1.7. The oxidative dehydrogenation catalyst of claim 1 , wherein the aspect ratio of the peak at 28.3±0.1 to the peak at 27±0.2 is about 0.65:1.8. The oxidative dehydrogenation catalyst of claim 1 , wherein the aspect ratio of the peak at 28.0±0.2 to the peak at 28.2±0.1 is 0.8:1 to 1.1:1.9. The oxidative dehydrogenation catalyst of claim 1 , wherein the aspect ratio of the peak at 28.0±0.2 to the peak at 28.2±0.1 is 0.9:1 to 1:1.10. The oxidative dehydrogenation catalyst of claim 1 , wherein the aspect ratio of the peak at 28.2±0.1 to the peak at 28.4 ...

CONVERSION OF MIXED METHANE/ETHANE STREAMS

The invention relates to a process for conversion of a stream comprising methane and ethane, comprising converting ethane from a stream comprising methane and ethane, in which stream the volume ratio of methane to ethane is of from 0.005:1 to 100:1, to a product having a vapor pressure at 0° C. lower than 1 atmosphere, resulting in a stream comprising methane and the product having a vapor pressure at 0° C. lower than 1 atmosphere; separating the product having a vapor pressure at 0° C. lower than 1 atmosphere from the stream comprising methane and the product having a vapor pressure at 0° C. lower than 1 atmosphere, resulting in a stream comprising methane; and chemically converting methane from the stream comprising methane, or feeding methane from the stream comprising methane to a network that provides methane as energy source, or liquefying methane from the stream comprising methane. 1. A process for conversion of a stream comprising methane and ethane , comprisingconverting ethane from a stream comprising methane and ethane, in which stream the volume ratio of methane to ethane is of from 0.005:1 to 100:1, preferably of from 0.2:1 to 100:1, more preferably of from 0.5:1 to 100:1, to a product having a vapor pressure at 0° C. lower than 1 atmosphere, resulting in a stream comprising methane and the product having a vapor pressure at 0° C. lower than 1 atmosphere;separating the product having a vapor pressure at 0° C. lower than 1 atmosphere from the stream comprising methane and the product having a vapor pressure at 0° C. lower than 1 atmosphere, resulting in a stream comprising methane; andchemically converting methane from the stream comprising methane or feeding methane from the stream comprising methane to a network that provides methane as energy source, or liquefying methane from the stream comprising methane.2. The process according to claim 1 , wherein when converting ethane to the product having a vapor pressure at 0° C. lower than 1 atmosphere claim ...

CATALYST FOR CONVERSION OF PROPYLENE TO PRODUCT COMPRISING A CARBOXYLIC ACID MOIETY

In accordance with the invention, there is provided a novel catalyst composition comprising MoVGaPdNbXY, wherein X comprises La, Te, Ge, Zn, In, or W; and Y comprises Al or Si; wherein Mo, V, Ga, Pd, Nb, La, Te, Ge, Zn, In, W, Al, or Si are optionally present in combination with oxygen; wherein the catalyst does not comprise an additional element that acts as a catalyst in the conversion of a propylene to the product. Also, disclosed is a method for the conversion of a propylene to a carboxylic acid moiety by contacting the propylene with the disclosed catalyst. 1. A catalyst for the conversion of a propylene to a product comprising a carboxylic acid moiety , wherein the catalyst comprises:{'br': None, 'MoVGaPdNbXY,'} X comprises La, Te, Ge, Zn, In, or W; and', 'Y comprises Al or Si;, 'wherein'} 'one or more of Mo, V, Ga, Pd, Nb, La, Te, Ge, Zn, In, W, Al, and/or Si are optionally present in combination with oxygen;', 'wherein'}wherein the catalyst does not comprise an additional element that acts as a catalyst in the conversion of the propylene to the product.2. The catalyst according to claim 1 , wherein the product does not comprise substantially any acrolein.3. The catalyst of claim 1 , wherein the product does not comprise any acrolein.4. The catalyst of claim 1 , wherein the additional element is a metal.5. The catalyst of claim 1 , wherein the additional element comprises Sb or Cs claim 1 , or a combination thereof.6. A catalyst for the conversion of a propylene to a product comprising a carboxylic acid moiety claim 1 , wherein the catalyst consists essentially of:{'br': None, 'MoVGaPdNbXY,'} X comprises La, Te, Ge, Zn, In, or W; and', 'Y comprises Al or Si;, 'wherein'} 'Mo, V, Ga, Pd, Nb, La, Te, Ge, Zn, In, W, Al, and/or Si are optionally present in combination with oxygen.', 'wherein'}7. The catalyst of claim 6 , wherein the catalyst is present on a support.8. The catalyst of claim 6 , wherein the catalyst comprises:{'br': None, 'sub': a', 'b', 'c', 'd', ' ...

OXIDATIVE DEHYDROGENATION CATALYST

Oxidative dehydrogenation catalysts comprising MoVNbTeO having improved consistency of composition and a 25% conversion of ethylene at less than 420° C. and a selectivity to ethylene above 95% are prepared by treating the catalyst precursor with HOin an amount equivalent to 0.30-2.8 mL HOof a 30% solution per gram of catalyst precursor prior to calcining. 1. A method to improve the consistency of an oxidative dehydrogenation catalyst of the empirical formula (measured by PIXE);{'br': None, 'sub': 1.0', '0.22-0.33', '0.10-0.16', '0.15-0.19', 'd, 'MoVTeNbO'}where d is a number to satisfy the valence of the oxide{'sub': 2', '2', '2', '2, 'comprising treating a precursor prior to calcining with HOin an amount equivalent to 0.30-2.8 mL HOof a 30% solution per gram of catalyst precursor.'}2. The method according to claim 1 , wherein the precursor is prepared by a method comprising:i) forming an aqueous solution of ammonium heptamolybdate (tetrahydrate) and telluric acid at a temperature from 30° C. to 85° C. and adjusting the pH of the solution to 6.5 to 8.5 with a nitrogen containing base to form soluble salts of the metals;ii) preparing a aqueous solution of vanadyl sulphate at a temperature from room temperature to 80° C.;iii) mixing the solutions from steps i) and ii) together;{'sub': 2', '4', '3, 'iv) slowly adding a solution of niobium monoxide oxalate (NbO(COH)) to the solution of step iii) to form a slurry;'}v) heating the resulting slurry in an autoclave under an inert atmosphere at a temperature from 150° C. to 190° C. for not less than 10 hours.3. The method according to claim 2 , the resulting solid from step v) is filtered and washed with deionized water claim 2 , and drying the washed solid for a time from 4 to 10 hours at a temperature from 70 to 100° C.4. The method according to claim 3 , further comprising calcining the catalyst in an inert atmosphere at a temperature from 200° C. to 600° C. for a time from 1 to 20 hours.5. The method according to claim 4 ...

Mechanically strong catalyst and catalyst carrier, its preparation, and its use

The invention concerns catalyst or a catalyst carrier comprising 35 to 99.9 wt % of metal oxide and 0.1 to 50 wt % of silanized silica particles, calculated on the total weight of the catalyst or catalyst carrier. The invention further relates to a process to prepare the catalyst or catalyst carrier. The invention also relates to the use of the catalyst, or a catalyst comprising the catalyst carrier, in a catalytic reaction.

SUPPORTED CATALYST FOR PRODUCTION OF UNSATURATED CARBOXYLIC ACIDS FROM ALKANES

The present disclosures and inventions relate to a supported catalyst composition for the catalytic oxidation of a hydrocarbon such as propane with oxygen or air, in the presence of a catalyst composition comprising a support material and a mixed metal composition comprising metals in the molar ratios described by the formula MoVGaPdNbZ, wherein the support material is neutral or oxidative. 1. A catalyst composition comprising a support material and a mixed metal composition comprising metals in the molar ratios described by the formula{'br': None, 'i': a', 'b', 'c', 'd', 'e', 'f,, 'MoVGaPdNbZ'}wherein a is 1,wherein b is from 0.01 to 0.9,wherein c is from than 0 to 0.2,wherein d is from 0.0000001 to 0.2,wherein e is greater than 0 to 0.2,wherein Z comprises La, Te, Ge, Zn, Si, In, or W, or a mixture thereof, andwherein f is greater than 0 to 0.5,wherein the support material is neutral or oxidative.2. The catalyst composition of claim 1 , wherein the support material comprises AlO claim 1 , SiO claim 1 , CeO claim 1 , TiO claim 1 , or ZrO claim 1 , or a mixture thereof.3. The catalyst composition of claim 1 , wherein the support material comprises CeO.4. The catalyst composition of claim 1 , wherein the support material comprises acetate-SiO claim 1 , low surface area TiO claim 1 , high surface area TiO claim 1 , acetate-AlO claim 1 , acetate-ZrO claim 1 , or actetate-CeO claim 1 , or a mixture thereof.5. The catalyst composition of claim 1 , wherein the support material is oxidative.6. The catalyst composition of claim 1 , wherein the support material is neutral.7. The catalyst composition of claim 1 , wherein the support material is a microporous or mesoporous support material.8. The catalyst composition of claim 1 , wherein the catalyst composition has a particle diameter size from 20 μm to 500 μm.9. The catalyst composition of claim 1 , wherein Z comprises Te.10. The catalyst composition of claim 1 , wherein the catalyst composition is stable to at least 600° C. ...

High Productivity Catalyst for Alkane Oxidation to Unsaturated Carboxylic Acids and Alkenes

The present disclosures and inventions relate to composite catalyst compositions for the catalytic oxidation of hydrocarbons such as propane with an oxygen containing stream, in the presence of a composite catalyst comprising CA that comprises at least components a metal M, a support S, and an optional alkali metal A, and also CB that comprises one or more mixed metal oxide phases comprising metals in the relative molar ratios indicated by the formula Mo a V b Ga c Pd d Nb e X f , to produce α,β-unsaturated carboxylic acids such as acrylic acid and/or olefins such as propylene.

Inherently safe odh operation

In the operation of an oxidative dehydrogenation (ODH) process, it is desirable to remove oxygen in the product stream for a number of reasons, including to reduce oxidation of the product. This may be achieved by having several pre-reactors upstream of the main reactor having a catalyst system containing labile oxygen. The feed passes through one or more reactors saturated with labile oxygen. When the labile oxygen is consumed through a valve system, the pre-reactor accepts product from the main reactor and complexes reactive oxygen in the product stream until the catalyst system is saturated with labile oxygen. Then the reactor becomes a pre-reactor and another pre-reactor becomes a scavenger.

Production of products from natural resources

The method disclosed herein relates to two stage catalytic processes for converting syngas to acetic acid, acrylic acid and/or propylene. More specifically, the method described and claimed herein relate to a method of producing acrylic acid and acetic acid comprising the steps of: a) providing a feedstream comprising syngas; b) contacting the feedstream with a first catalyst to produce a first product stream comprising C 2 -C 3 olefins and/or C 2 -C 3 paraffins; and c) contacting the first product stream with oxygen gas and a second catalyst, thereby producing a second product stream comprising acrylic acid and acetic acid, wherein there is no step for separating the components of the first product stream before the first product stream is contacted with the second catalyst.

PHOTO-CATALYTIC SYSTEMS FOR THE PRODUCTION OF HYDROGEN

A system and method for splitting water to produce hydrogen and oxygen employing sunlight energy are disclosed. Hydrogen and oxygen may then be stored for later use as fuels. The system and method use inorganic capping agents that cap the surface of semiconductor nanocrystals to form photocatalytic capped colloidal nanocrystals, which may be deposited on a substrate and treated to form a photoactive material. The photoactive material may be employed in the system to harvest sunlight and produce energy necessary for water splitting. The system may also include elements necessary to collect, transfer and store hydrogen and oxygen, for subsequent transformation into electrical energy. 1. A method for producing photocatalytic capped colloidal nanocrystals , comprisingreacting a semiconductor nanocrystals precursor and an organic solvent to produce organic capped semiconductor nanocrystals; dissolving the inorganic capping agent in a first solvent to produce a first solution;', 'dissolving the organic capped nanocrystals in a second solvent to produce a second solution;', 'combining the first solution and the second solution in a single vessel;', 'reacting the first solution with the second solution, whereby a portion of the organic capping agent is displaced by inorganic capping agent;', 'continuing reacting until the combination reaches equilibrium;, 'substituting an inorganic capping agent for the organic capping agent, including'}allowing the combination to stabilize; andprecipitating photocatalytic capped colloidal nanocrystals from the combination.2. The method of claim 1 , wherein the organic solvent is a stabilizing organic ligand.3. The method of claim 1 , wherein the organic solvent is trioctylphosphine oxide.4. The method of claim 1 , wherein the organic solvent is one of a long-chain aliphatic amines claim 1 , long-chain aliphatic phosphines claim 1 , long-chain aliphatic carboxylic acids claim 1 , long-chain aliphatic phosphonic acids and mixtures thereof.5. ...

Catalysts for the oxidative dehydrogenation of alkanes

This document relates to oxidative dehydrogenation catalysts that include molybdenum, vanadium, and oxygen.

Low pressure gas release hydrothermal and peroxide treatment of odh catalyst

The preparation of an oxidative dehydrogenation catalyst comprising Mo, V, Nb and Te using a hydrothermal step. In some embodiments, the activity and reproducibility of the catalyst is improved by conducting the hydrothermal step while permitting gaseous products to leave the reactor. In some instances a condenser may be upstream of the outlet of the reactor.

Oxidation catalyst preparation

A method for producing a catalyst by contacting a starting mixed metal oxide catalyst with an aqueous solution comprising oxalic acid and a metal oxide precursor to form a post-treated mixed metal oxide catalyst.

SILICA-SUPPORTED CATALYST

A silica-supported catalyst used when producing a corresponding unsaturated nitrile in a vapor-phase catalytic ammoxidation reaction of propane or isobutane, the catalyst including a metal oxide represented by the following formula (1), 1. A silica-supported catalyst used when producing a corresponding unsaturated nitrile in a vapor-phase catalytic ammoxidation reaction of propane or isobutane , the catalyst comprising a metal oxide represented by the following formula (I) ,{'br': None, 'sub': a', 'b', 'c', 'd', 'e', 'n, 'MoVNbXTZO\u2003\u2003(1)'}(wherein X represents at least one or more elements selected from Sb and Te; T represents at least one or more elements selected from Ti, W, Mn, and Bi; Z represents at least one or more elements selected from La, Ce, Yb, and Y; and a, b, c, d, and e are in a range of 0.05≦a≦0.5, 0.01≦b≦0.5, 0.001≦c≦0.5, 0≦d≦1, and 0≦e≦1, respectively, and n represents a value that satisfies an atomic valence){'sup': 3', '2, 'wherein the silica-supported catalyst has an average pore size of 60 to 120 nm, a total pore volume of 0.15 cm/g or more, a specific surface area of 5 to 25 m/g, and a crystallite size of 40 to 250 nm as determined from half width of a (001) peak by X-ray diffraction.'}2. The silica-supported catalyst according to claim 1 , wherein a pore volume of pores having a pore size of less than 60 nm based on total pore volume is less than 30% claim 1 , and a pore volume of pores having a pore size exceeding 120 nm based on total pore volume is less than 30%.3. The silica-supported catalyst according to or claim 1 , wherein a support amount of the silica is 20 to 70% by mass based on total mass of the catalyst composed of the metal oxide and the silica.4. A method for producing a silica-supported catalyst claim 1 , comprising the steps of:(I) preparing a raw material-prepared solution containing Mo, V, Nb, X, T, and Z, wherein an atomic ratio a of V to one Mo atom is 0.05≦a≦0.5, an atomic ratio b of Nb to one Mo atom is 0.01≦b ...

CATALYST FOR ALKANE OXIDATIVE DEHYDROGENATION AND/OR ALKENE OXIDATION

The invention relates to a process for treating a catalyst for alkane oxidative dehydrogenation and/or alkene oxidation, which catalyst is a mixed metal oxide catalyst containing molybdenum, vanadium and niobium, wherein the process comprises: contacting the catalyst with a gas mixture comprising an inert gas and oxygen (02), wherein the amount of oxygen is of from 10 to less than 10,000 parts per million by volume (ppmv), based on the total volume of the gas mixture, at an elevated temperature. 1. A process for treating a catalyst for alkane oxidative dehydrogenation and/or alkene oxidation , which catalyst is a mixed metal oxide catalyst containing molybdenum , vanadium and niobium , wherein the process comprises:contacting the catalyst with a gas mixture comprising an inert gas and oxygen (O2), wherein the amount of oxygen is of from 10 to less than 10,000 parts per million by volume (ppmv), based on the total volume of the gas mixture, at an elevated temperature.2. A process according to claim 1 , wherein the temperature is of from 300 to 900° C.3. A process according to claim 1 , wherein the amount of oxygen is of from 100 to 9 claim 1 ,500 parts per million by volume.4. A process according to claim 1 , wherein the catalyst additionally contains tellurium.5. A process for preparing a catalyst for alkane oxidative dehydrogenation and/or alkene oxidation claim 1 , which catalyst is a mixed metal oxide catalyst containing molybdenum claim 1 , vanadium and niobium claim 1 , wherein the process comprises:a) preparing a catalyst containing molybdenum, vanadium and niobium;b) contacting the catalyst with oxygen (O2) at an elevated temperature, to obtain a mixed metal oxide catalyst containing molybdenum, vanadium and niobium; andc) contacting the catalyst with a gas mixture comprising an inert gas and oxygen (O2), wherein the amount of oxygen is of from 10 to less than 10,000 parts per million by volume (ppmv), based on the total volume of the gas mixture, at an ...

AGGLOMERATED ODH CATALYST

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

TREATMENT OF A MIXED METAL OXIDE CATALYST CONTAINING MOLYBDENUM, VANADIUM, NIOBIUM AND OPTIONALLY TELLURIUM

The invention relates to a process for treatment of a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium, comprising contacting a gas stream comprising methane, an inert gas or oxygen or any combination of two or more of these with the catalyst, wherein said gas stream comprises 0 to 25 vol. % of an alkane containing 2 to 6 carbon atoms and/or alkene containing 2 to 6 carbon atoms. 1. A process for treatment of a mixed metal oxide catalyst containing molybdenum , vanadium , niobium and optionally tellurium , comprising contacting a gas stream comprising methane , an inert gas or oxygen or any combination of two or more of these with the catalyst , wherein said gas stream comprises 0 to 25 vol. % of an alkane containing 2 to 6 carbon atoms and/or alkene containing 2 to 6 carbon atoms.2. The process according to claim 1 , wherein the temperature is of from 200 to 500° C.3. The process according to claim 2 , wherein the temperature is of from 250 to 500° C.4. The process according to claim 1 , wherein the pressure is of from 0.1 to 15 bara. preferably of from 1 to 5 bara.5. The process according to claim 1 , wherein the catalyst is a fresh catalyst.6. The process according to claim 5 , wherein the fresh catalyst is intended to be used as a catalyst in the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms.7. The process according to claim 1 , wherein the catalyst is a used catalyst.8. The process according to claim 7 , wherein the used catalyst has been used as a catalyst in the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms. The present invention relates to a process for treatment of a mixed metal oxide catalyst containing molybdenum (Mo), vanadium (V), niobium (Nb) and optionally tellurium (Te).Mixed metal oxide catalysts containing molybdenum, vanadium, ...

ALKANE OXIDATIVE DEHYDROGENATION AND/OR ALKENE OXIDATION

The invention relates to a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms, comprising contacting a first gas stream comprising oxygen and the alkane containing 2 to 6 carbon atoms and/or the alkene containing 2 to 6 carbon atoms with a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium; followed by contacting a second gas stream comprising methane, an inert gas or oxygen or any combination of two or more of these with the catalyst, wherein the second gas stream comprises 0 to 25 vol. % of the alkane containing 2 to 6 carbon atoms and/or alkene containing 2 to 6 carbon atoms. 1. A process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms , comprisingcontacting a first gas stream comprising oxygen and the alkane containing 2 to 6 carbon atoms and/or the alkene containing 2 to 6 carbon atoms with a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium; followed bycontacting a second gas stream comprising methane, an inert gas or oxygen or any combination of two or more of these with the catalyst, wherein the second gas stream comprises 0 to 25 vol. % of the alkane containing 2 to 6 carbon atoms and/or alkene containing 2 to 6 carbon atoms.2. The process according to claim 1 , wherein the temperature during the entire process is of from 300 to 500° C.3. The process according to claim 2 , wherein the temperature is of from 310 to 450° C.4. The process according to claim 1 , wherein the pressure during the entire process is of from 0.1 to 15 bara.5. The process according to claim 1 , wherein the process is a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and wherein said alkane is ethane or propane.6. The process according to claim 1 , wherein the process is a ...

ALKANE OXIDATIVE DEHYDROGENATION AND/OR ALKENE OXIDATION

The invention relates to a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms, comprising contacting a first gas stream comprising methane, an inert gas or oxygen or any combination of two or more of these, wherein the first gas stream comprises 0 to 2 vol. % of the alkane containing 2 to 6 carbon atoms and/or alkene containing 2 to 6 carbon atoms, with a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium; followed by contacting a second gas stream comprising oxygen and the alkane containing 2 to 6 carbon atoms and/or the alkene containing 2 to 6 carbon atoms with the catalyst. 1. A process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms , comprisingcontacting a first gas stream comprising methane, an inert gas or oxygen or any combination of two or more of these, wherein the first gas stream comprises 0 to 25 vol. % of the alkane containing 2 to 6 carbon atoms and/or alkene containing 2 to 6 carbon atoms, with a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium; followed bycontacting a second gas stream comprising oxygen and the alkane containing 2 to 6 carbon atoms and/or the alkene containing 2 to 6 carbon atoms with the catalyst.2. The process according to claim 1 , wherein the temperature during the entire process is of from 200 to 500° C.3. The process according to claim 2 , wherein the temperature is of from 310 to 450° C.4. The process according to claim 1 , wherein the pressure during the entire process is of from 0.1 to 15 bara.5. The process according to claim 1 , wherein the catalyst that is contacted with the first gas stream is a fresh catalyst or a used catalyst.6. The process according to claim 1 , wherein the process is a process of the oxidative dehydrogenation of an alkane ...

CONVERSION OF ALCOHOLS TO CARBOXYLIC ACIDS USING HETEROGENEOUS PALLADIUM-BASED CATALYSTS

Disclosed are methods for synthesizing an ester or a carboxylic acid from an organic alcohol. To form the ester one reacts, in the presence of oxygen gas, the alcohol with methanol or ethanol. This reaction occurs in the presence of a catalyst comprising palladium and a co-catalyst comprising bismuth, tellurium, lead, cerium, titanium, zinc and/or niobium (most preferably at least bismuth and tellurium). Alternatively that catalyst can be used to generate an acid from that alcohol, when water is also added to the reaction mix. 1. A method for synthesizing an acid from an alcohol , comprising:{'sub': '2', 'exposing a compound of the formula R—CH—OH to oxygen gas and methanol-water mixture so as to yield a compound of the formula RCOOH;'}wherein said exposing is in the presence of a catalyst comprising palladium, bismuth and tellurium;wherein R is an alkyl, cyclic, aryl, heterocyclic, arene, amine, ether, or ester, with or without sulfur or halogen content.2. The method of claim 1 , wherein the catalyst further comprises an elemental carbon support in the form of charcoal or activated carbon.3. The method of claim 1 , wherein there is at least 0.1 mol percent palladium claim 1 , at least 0.01 mol percent bismuth claim 1 , and at least 0.01 mol percent tellurium in the catalyst.4. The method of claim 1 , in which the bismuth is present in a salt form and the tellurium is present in a metal form.5. The method of claim 4 , wherein the bismuth salt is Bi(NO).5HO.6. A method for synthesizing an acid from an alcohol claim 4 , comprising:{'sub': '2', 'exposing a compound of the formula R—CH—OH to oxygen gas and water so as to yield a compound of the formula RCOOH;'}wherein said exposing is in the presence of a catalyst comprising palladium and a co-catalyst comprising at least two of the following: bismuth, tellurium, lead, cerium, titanium, zinc and niobium;wherein R is an alkyl, cyclic, aryl, heterocyclic, arene, amine, ether, or ester, with or without sulfur or halogen ...

CONTROLLING CARBON DIOXIDE OUTPUT FROM AN ODH PROCESS

In some embodiments provided herein are processes for controlling carbon dioxide output levels coming from an oxidative dehydrogenation (ODH) process. Carbon dioxide output from an ODH process includes that produced in the ODH reaction and carry over when carbon dioxide is used as an inert diluent. Under certain circumstances carbon dioxide can also be consumed in the ODH process by acting as an oxidizing agent. By varying the amount of steam introduced into the ODH process an operator may alter the degree to which carbon dioxide acts as an oxidizing agent. This in turn allows a level of control in the degree to which carbon dioxide is consumed in the process, effecting overall carbon dioxide output. Minimizing the carbon dioxide output provides an opportunity to limit or eliminate the requirement for release of carbon dioxide into the atmosphere. 1. A method for controlling the carbon dioxide output from an oxidative dehydrogenation process comprising the steps of:i) introducing a gas mixture comprising a lower alkane and oxygen, and optionally one or more of steam and inert diluent, into at least one ODH reactor containing the same or different ODH catalysts, provided that if more than one ODH reactor is present then at least one of the ODH catalysts is capable of utilizing carbon dioxide as an oxidizing agent, under conditions to produce a product stream from at least one ODH reactor comprising corresponding alkene, and optionally one or more of unreacted lower alkane, unreacted oxygen, carbon dioxide, carbon monoxide, inert diluent, and acetic acid;ii) measuring carbon dioxide levels in one or more said product streams; and a. introducing steam, or increasing amount of steam introduced, into the at least one ODH reactor in an amount sufficient to decrease the carbon dioxide output levels when the measured carbon dioxide level is above a predetermined target carbon dioxide level;', 'b. decreasing the flow rate of steam introduced into the at least one ODH reactor ...

Catalyst Material for the Oxidation of Hydrocarbons

A catalyst material for the oxidation and/or oxidative dehydrogenation of hydrocarbons, in particular for the selective oxidation of propane to acrylic acid, is specified, comprising a) molybdenum (Mo), b) vanadium (V), c) niobium (Nb), d) tellurium (Te), e) nickel (Ni), f) tungsten (W) and g) manganese (Mn), in which the molar ratio of at least one element, which is selected from nickel, tungsten and manganese, to molybdenum lies in the range 0.01 to 0.2, more preferably 0.05 to 0.15 and particularly preferably from 0.0025:1 to 0.3:1. Furthermore, a catalyst for the oxidation and/or oxidative dehydrogenation of hydrocarbons, a use of the catalyst material or of the catalyst, a method for producing a catalyst material for the oxidation and/or oxidative dehydrogenation of hydrocarbons and a method for the selective oxidation of propane to acrylic acid is specified. 2. Catalyst material according to claim 1 , in which the molar ratio of at least one element claim 1 , which is selected from vanadium claim 1 , niobium and tellurium claim 1 , to molybdenum lies in the range of from 0.15:1 to 0.3:1 or 0.17:1 to 0.27:1; and/or with an X-ray diffractogram which has diffraction reflexes h claim 1 , i claim 1 , k and l the peaks of which lie at the diffraction angles (2θ) 26.2±0.5 (h) claim 1 , 27.0±0.5 (i) claim 1 , 7.8±0.5 (k) and 28.0±0.5 (l); and/or{'sub': h', 'i', 'k', 'l', 'x (x=1 to 3), 'claim-text': [{'br': None, 'i': R', '=P', 'P', '+P, 'sub': 1', 'h', 'h', 'i, '/()>0.3, preferably >0.35 and particularly preferably >0.4; and/or'}, {'br': None, 'i': R', '=P', 'P', '+P, 'sub': 2', 'i', 'i', 'l, '/()>0.5, preferably >0.6 and particularly preferably >0.63; and/or'}, {'br': None, 'i': R', '=P', 'P', '+P, 'sub': 3', 'i', 'i', 'k, '/()<0.8, preferably <0.75, particularly preferably <0.7; and/or'}], 'in which the intensities P, P, P, Pof the diffraction reflexes h, i, k and l of the X-ray diffractogram satisfy the following equations, with Ras the intensity ratio defined by ...

FACILITATED CO2 TRANSPORT MEMBRANE AND METHOD FOR PRODUCING SAME, AND METHOD AND APPARATUS FOR SEPARATING CO2

Provided is a facilitated COtransport membrane having an improved COpermeance and an improved CO/Hselectivity. The facilitated COtransport membrane includes a separation-functional membrane that includes a hydrophilic polymer gel membrane containing a COcarrier and a COhydration catalyst. Further preferably, the COhydration catalyst at least has catalytic activity at a temperature of 100° C. or higher, has a melting point of 200° C. or higher, or is soluble in water. 1. A facilitated COtransport membrane comprising a separation-functional membrane that includes a hydrophilic polymer gel membrane containing a COcarrier and a COhydration catalyst.2. The facilitated COtransport membrane according to claim 1 , wherein the COhydration catalyst has catalytic activity at a temperature of 100° C. or higher.3. The facilitated COtransport membrane according to claim 1 , wherein the COhydration catalyst has a melting point of 200° C. or higher.4. The facilitated COtransport membrane according to claim 1 , wherein the COhydration catalyst is soluble in water.5. The facilitated COtransport membrane according to claim 1 , wherein the COhydration catalyst contains an oxo acid compound.6. The facilitated COtransport membrane according to claim 5 , wherein the COhydration catalyst is an oxo acid compound of at least one element selected from group 6 elements claim 5 , group 14 elements claim 5 , group 15 elements and group 16 elements.7. The facilitated COtransport membrane according to claim 1 , wherein the COhydration catalyst contains at least one of a tellurous acid compound claim 1 , a selenious acid compound claim 1 , an arsenious acid compound and an orthosilicic acid compound.8. The facilitated COtransport membrane according to claim 1 , wherein the COhydration catalyst contains a molybdic acid compound.9. The facilitated COtransport membrane according to claim 1 , wherein the gel membrane is a hydrogel.10. The facilitated COtransport membrane according to claim 1 , wherein ...

Catalyst Compositions Including Metal Chalcogenides, Processes for Forming the Catalyst Compositions, and Uses Thereof

Aspects of the present disclosure generally relate to catalyst compositions including metal chalcogenides, processes for producing such catalyst compositions, processes for enhancing catalytic active sites in such catalyst compositions, and uses of such catalyst compositions in, e.g., processes for producing conversion products. In an aspect, a process for forming a catalyst composition is provided. The process includes introducing an electrolyte material and an amphiphile material to a metal chalcogenide to form the catalyst composition. In another aspect, a catalyst composition is provided. The catalyst composition includes a metal chalcogenide, an electrolyte material, and an amphiphile material. Devices for hydrogen evolution reaction are also provided. 1. A process for forming a catalyst composition , comprising introducing an electrolyte material and an amphiphile material to a metal chalcogenide to form the catalyst composition.2. The process of claim 1 , further comprising introducing a voltage to the to the catalyst composition.3. The process of claim 1 , wherein a first amount of hydrogen atoms absorbed on the metal chalcogenide before introducing the electrolyte material and the amphiphile material is less than a second amount of hydrogen atoms absorbed on the metal chalcogenide after introducing the electrolyte material and the amphiphile material.4. The process of claim 1 , wherein the metal chalcogenide comprises a density of chalcogen atom vacancies from about 6% to about 30% claim 1 , as determined by x-ray photoelectron spectroscopy.5. The process of claim 1 , wherein:the electrolyte material comprises an acid; andthe amphiphile material comprises an anionic compound.6. The process of claim 5 , wherein the acid has a pKa of about 3 or less as determined by potentiometric titration.8. The process of claim 7 , wherein:M is selected from the group consisting of Mo, W, Nb, Ni, Fe, V, Cr, Mn, and combinations thereof; andE is selected from the group ...

OXIDATIVE ESTERIFICATION PROCESS

A process for producing methyl methacrylate, the process comprising contacting reactants comprising methacrolein, methanol and an oxygen-containing gas, under reaction conditions in the presence of a solid catalyst comprising palladium, bismuth and tellurium, wherein the solid catalyst further comprises a support selected from at least one member of the group consisting of silica, and alumina, with the proviso that the process produces less than 1 mole methyl formate per mole of methyl methacrylate. 1. A process for producing methyl methacrylate , the process comprising contacting reactants comprising methacrolein , methanol and an oxygen-containing gas , under reaction conditions in the presence of a solid catalyst comprising palladium , bismuth and tellurium , wherein the solid catalyst further comprises a support selected from at least one member of the group consisting of silica , and alumina , with the proviso that the process produces less than 1 mole methyl formate per mole of methyl methacrylate.2. The process of wherein the solid catalyst further comprises a support selected from at least one member of the group consisting of pyrogenic silica claim 1 , silica gel claim 1 , alpha alumina and gamma alumina.3. The process of wherein the process produces less than 0.8 mole methyl formate per mole of methyl methacrylate.4. The process of wherein the process produces less than 0.6 mole methyl formate per mole of methyl methacrylate.5. The process of wherein the process produces less than 0.4 mole methyl formate per mole of methyl methacrylate.6. The process of wherein the process produces less than 0.2 mole methyl formate per mole of methyl methacrylate.7. The process of wherein the support comprises pyrogenic silica.8. The process of the support comprises gamma alumina.9. The process of wherein the ratio of methanol to methacrolein is from 1:1 to 10:1 mole percent.10. The process of wherein the reacting is conducted in the presence of a polymerization inhibitor. ...

CATALYST FOR ETHANE ODH

A catalyst for oxidative dehydrogenation (ODH) of ethane with an empirical formula Mo—V—Te—Nb—Pd—O produced using a process comprising impregnation of the Pd component on the surface of the catalyst following a calcination step using a Pd compound free of halogens. The resulting catalyst can be used in both diluted and undiluted ODH processes and shows higher than expected activity without any loss of selectivity. 1. An oxidative dehydrogenation catalyst comprising a mixed metal oxide having the empirical formula{'br': None, 'sub': a', 'b', 'c', 'd', 'e', 'f, 'MoVTeNbPdO'} a, b, c, d, e, and f are the relative atomic amounts of the elements Mo, V, Te, Nb, Pd and O, respectively; and', 'when a=1, b=0.01 to 1.0, c=0.01 to 1.0, d=0.01 to 1.0, 0.001 Подробнее

CATALYST FOR ETHANE ODH

A catalyst for oxidative dehydrogenation (ODH) of ethane with an empirical formula Mo—V—Te—Nb—Pd—O produced using a process comprising impregnation of the Pd component on the surface of the catalyst following a calcination step using a Pd compound free of halogens. The resulting catalyst can be used in both diluted and undiluted ODH processes and shows higher than expected activity without any loss of selectivity. 1. A process for preparing an oxidative dehydrogenation catalyst comprising a mixed metal oxide having the empirical formula{'br': None, 'sub': a', 'b', 'c', 'd', 'e', 'f, 'MoVTeNbPdO'} a, b, c, d, e and f are the relative atomic amounts of the elements Mo, V, Te, Nb, Pd, and O, respectively; and', 'a is 1, b is from 0.01 to 1.0, c is from 0.01 to 1.0, d is from 0.01 to 0.1.0, e is from 0.0001 to less than 0.10, and f is dependent on the oxidation state of the other elements;, 'wherein'} admixing compounds of elements Mo, V, Te, and Nb, in a solvent comprising water to produce a first mixture;', 'heating the first mixture in a first pressurized vessel at a temperature of from 100° C. to 200° C.;', 'recovering a first insoluble material from the first pressurized vessel;', 'subjecting the first recovered insoluble material to a calcining at a temperature of from 500° C. to 700° C. under an inert atmosphere to produce a calcined product;', {'sub': 3', '4', '3', '2', '3', '2', '3', '2, 'contacting the calcined product with an aqueous solution comprising a Pd compound to form second mixture, wherein the aqueous solution comprising the Pd compound is prepared from a Pd compound chosen from [Pd(NH)](NO), Pd(HCO), Pd(CHCOO)an analogous Pd containing salt, or a combination thereof;'}, 'subjecting the second mixture to drying; and', 'recovering a second insoluble material from provide the catalyst, and', 'wherein the process excludes calcination after the impregnation of Pd., 'the process comprising2. The process of claim 1 , wherein the first mixture in the first ...

CATALYSTS FOR PETROCHEMICAL CATALYSIS

Metal oxide catalysts comprising various dopants are provided. The catalysts are useful as heterogenous catalysts in a variety of catalytic reactions, for example, the oxidative coupling of methane to C2 hydrocarbons such as ethane and ethylene. Related methods for use and manufacture of the same are also disclosed. 1. A catalyst comprising a mixed oxide of magnesium and manganese , wherein the catalyst further comprises lithium and boron dopants and at least one doping element from groups 4 , 9 , 12 , 13 or combinations thereof , wherein the catalyst comprises a Cselectivity of greater than 50% and a methane conversion of greater than 20% when the catalyst is employed as a heterogeneous catalyst in the oxidative coupling of methane at a temperature of 750° C. or less.2. The catalyst of claim 1 , wherein the catalyst further comprises a sodium dopant.3. The catalyst of claim 1 , wherein the at least one doping element is cobalt.4. The catalyst of claim 1 , wherein the at least one doping element is gallium.5. The catalyst of any of claim 1 , wherein the catalyst further comprises at least one additional doping element from group 2.6. The catalyst of claim 5 , wherein the at least one additional doping element is beryllium claim 5 , barium claim 5 , hafnium or aluminum.7. A catalyst comprising a mixed oxide of manganese and tungsten claim 5 , wherein the catalyst further comprises a sodium dopant and at least one doping element from groups 2 claim 5 , 16 or combinations thereof.8. The catalyst of claim 7 , wherein the catalyst comprises a Cselectivity of greater than 50% and a methane conversion of greater than 20% when the catalyst is employed as a heterogenous catalyst in the oxidative coupling of methane at a temperature of 750° C. or less.9. The catalyst of claim 7 , wherein the doping element is barium claim 7 , beryllium or tellurium.10. A catalyst comprising an oxide of a rare earth element claim 7 , wherein the catalyst further comprises at least one doping ...

Method of increasing the thickness of colloidal nanosheets and materials consisting of said nanosheets

A process of growth in the thickness of at least one facet of a colloidal inorganic sheet. By sheet is meant a structure having at least one dimension, the thickness, of nanometric size and lateral dimensions great compared to the thickness, typically more than 5 times the thickness. By homostructured is meant a material of homogeneous composition in the thickness and by heterostructured is meant a material of heterogeneous composition in the thickness. The process allows the deposition of at least one monolayer of atoms on at least one inorganic colloidal sheet, this monolayer being constituted of atoms of the type of those contained or not in the sheet. Homostructured and heterostructured materials resulting from such process as well as the applications of the materials are also described.

PROCESS FOR PREPARING A CATALYST, CATALYST AND PROCESS FOR THE OXIDATIVE DEHYDROGENATION OF HYDROCARBONS

A process for preparing a catalyst provided in the form of a metal oxide catalyst having at least one element selected from Mo, Te, Nb, V, Cr, Dy, Ga, Sb, Ni, Co, Pt and Ce. The catalyst is subjected to an aftertreatment to increase the proportion of the M1 phase, by contacting the catalyst with steam at a pressure below 100 bar or by contacting the catalyst with oxygen to obtain an aftertreated catalyst. The aftertreated catalyst may be used for oxidative dehydrogenation processes. 1. A process for preparing a catalyst , wherein a catalyst is provided in the form of a metal oxide catalyst which comprises at least one element of the group Mo , Te , Nb , V , Cr , Dy , Ga , Sb , Ni , Co , Pt and Ce ,characterized in that is contacted with steam at a pressure below 100 bar, preferably below 80 bar, preferably below 50 bar, and/or', 'is contacted with oxygen., 'the catalyst is subjected to an aftertreatment to increase the fraction of the M1 phase of the catalyst, wherein the catalyst, with generation of an aftertreated catalyst,'}2. The process as claimed in claim 1 , characterized in that the catalyst claim 1 , during the aftertreatment claim 1 , is contacted with the steam and/or the oxygen at a temperature of at least 200° C. claim 1 , preferably at a temperature of at least 350° C. claim 1 , preferably at a temperature of at least 400° C. claim 1 , preferably at a temperature in the range from 200° C. to 650′ claim 1 , preferably at a temperature in the range from 300° C. to 650° C. claim 1 , preferably at a temperature in the range from 350° C. to 600° C. claim 1 , preferably at a temperature in the range from 350° C. to 550° C. claim 1 , preferably at a temperature in the range from 350° C. to 400° C. claim 1 , preferably at a temperature in the range from 400° C. to 500° C.3. The process as claimed in claim 1 , characterized in that the catalyst is a metal oxide catalyst comprising the elements Mo claim 1 , V claim 1 , Te claim 1 , Nb.4. The process as claimed ...

Heterogeneous catalysts for the transesterification of aromatic alcohols; and methods of making and use thereof

Disclosed herein are new mixed metal oxide catalysts suitable as heterogeneous catalysts for catalyzing the transesterification process of aromatic alcohols with a dialkyl carbonate to form aromatic carbonates. The heterogeneous catalyst comprises a combination of two, three, four, or more oxides of Mo, V, Nb, Ce, Cu, Sn, or an element selected from Group IA or Group IIA of the periodic table.

HIGH CONVERSION AND SELECTIVITY ODH PROCESS

Ethane may be catalytically oxidatively dehydrogenated to ethylene at high conversions and high selectivity in a circulating fluidized bed (CFB) reactor in the presence of oxygen in the feed in an amount above the flammability limit. The reactor has an attached regeneration reactor to regenerate the catalyst and cycle back to the CFB. 2. The process according to claim 1 , wherein the oxidative dehydrogenation reactor comprises a riser and the regeneration reactor is a separate fluidized bed reactor claim 1 , said regeneration reactor being connected with said riser to flow oxidized catalyst back to said riser.3. The process according to claim 2 , wherein the top of said riser comprises a distributor system.4. The process according to claim 3 , further comprising passing one or more of low temperature steam and atomized water into said catalyst flow into said riser to cool the catalyst to control the heat balance of the of the oxidative dehydrogenation reactor.5. The process according to claim 3 , wherein there is a downcomer between said oxidative dehydrogenation reactor and said regeneration reactor to flow reduced catalyst from said oxidative dehydrogenation reactor to said regeneration reactor.6. The process according to claim 5 , further comprising passing low temperature steam counter current to the flow of oxygen depleted catalyst through said downcomer to strip entrained alkane feed and product.7. The process according to claim 6 , further comprising passing air or a mixture of air and nitrogen through the regeneration reactor in an amount to substantially extract the oxygen from the air or a mixture of air and nitrogen and generating a gas product stream comprising not less than 80-100% of nitrogen.8. The process according to claim 7 , further comprising recycling a portion of the oxygen reduced effluent stream from the regenerator reactor and optionally cooling it and recycling it to the regenerator reactor.9. The process according to claim 7 , further ...

Calcination Process to Produce Enhanced ODH Catalyst

Mixed metal oxide catalysts having an amorphous content of not less than 40 wt. % are prepared by calcining the catalyst precursor fully or partially enclosed by a porous material having a melting temperature greater than 600° C. in an inert container including heating the catalyst precursor at a rate from 0.5 to 10° C. per minute from room temperature to a temperature from 370° C. to 540° C. under a stream of pre heated gas chosen from steam and inert gas and mixtures thereof at a pressure of greater than or equal to 1 psig having a temperature from 300° C. to 540° C. and holding the catalyst precursor at that temperature for at least 2 hours and cooling the catalyst precursor to room temperature. 1. A method to calcine a catalyst precursor of the formula{'br': None, 'sub': 1', '0.1-1', '0.1-1', '0.01-0.2', '0.2', 'd, 'MoVNbTeXO'} calcining the catalyst precursor in an inert container with flow passage there through, at a rate from 0.5 to 10° C. per minute from room temperature to a holding temperature from 370° C. to 540° C. under a stream of pre heated gas chosen from steam and inert gas and mixtures thereof at a rate of flow comparable to a flow rate of not less 150 sccm through a 2.54 cm diameter tube, with a length of 152 cm at a pressure of greater than or equal to 1 psig having a temperature from 300° C. to 540° C.;', 'cooling the catalyst precursor to room temperature said catalyst precursor being fully or partially enclosed by a porous material having a melting temperature greater than 600° C.', 'holding the catalyst precursor at the holding temperature for at least 2 hours; and'}], 'where X is chosen from Pd, Sb Ba, Al, W, Ga, Bi, Sn, Cu, Ti, Fe, Co, Ni, Cr, Zr, Ca, oxides thereof and mixtures thereof, and d is a number to satisfy the valence of the catalyst while maintaining an amorphous content of not less than 40 wt. % the method comprising'}2. The method according to claim 1 , wherein the inert container is made from high temperature glass claim 1 , ...

HIGH-PERFORMANCE POLYOXOMETALATE CATALYST AND METHOD OF PREPARING THE SAME

The present invention relates to a high-performance polyoxometalate catalyst and a method of preparing the same. More particularly, the present invention provides a high-performance polyoxometalate catalyst, the activity and selectivity of which may be improved by controlling the content of vanadium and the like and which has superior reproducibility and may unsaturated carboxylic acid from unsaturated aldehyde in a high yield for a long time, a method of preparing the same, and the like. 1. A polyoxometalate catalyst , comprising a metal oxide represented by Formula 1 below:{'br': None, 'sub': a', 'b', 'c', 'd', 'e', 'f', 'g, 'MOAVBCDO,\u2003\u2003[Formula 1]'}wherein A is one or more elements selected from the group consisting of W and Cr; B is one or more elements selected from the group consisting of P, As, B, Sb, Ce, Pb, Mn, Nb and Te; C is one or more elements selected from the group consisting of Si, Al, Zr, Rh, Cu, Ni, Ti, Ag, Fe, Co and Sn; D is one or more selected from the group consisting of Na, K, Li, Rb, Cs, Ta, Ca, Mg, Sr and Ba; and a, b, c, d, e, f, and g represent atomic ratios of the respective elements,wherein, when a=12, b is 0.01 to 15; c is 0.01 to 15, d is 0 to 20, e is 0 to 20, f is 0 to 20; and g is determined depending upon oxidation states of the respective ingredients, andwherein a mole ratio of V to A (V/A) is 0.01 to 10.2. The polyoxometalate catalyst according to claim 1 , wherein each of d claim 1 , e and f is 0.01 to 20.3. The polyoxometalate catalyst according to claim 1 , wherein the vanadium (V) comprises 30% or more of vanadium having an oxidation number of 4+.4. The polyoxometalate catalyst according to claim 1 , wherein the polyoxometalate catalyst comprises an inert carrier claim 1 , as a supporter of the metal oxide.5. The polyoxometalate catalyst according to claim 4 , wherein a loading amount of a metal oxide coated on the inert carrier is 30 to 80% by weight.6. The polyoxometalate catalyst according to claim 1 , wherein ...

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

The invention relates to a catalyst comprising an active component based on molybdenum and on potassium and a support based on hydroxyapatite, and also to a process for preparing said catalyst and a process for producing methyl mercaptan in a catalytic process by reaction of carbon monoxide, sulphur and/or hydrogen sulphide and hydrogen, comprising the use of said catalyst. 110-. (canceled)11. A catalyst comprising a molybdenum- and potassium-based active component and a hydroxyapatite-based support.12. The catalyst of claim 11 , wherein the catalyst support is hydroxyapatite having stoichiometric formula Ca(PO)(OH).13. The catalyst of claim 12 , wherein the molybdenum- and potassium-based active component is selected from the group consisting of compounds based on Mo—S—K claim 12 , compounds based on Mo—O—K claim 12 , and mixtures thereof.14. The catalyst of claim 13 , wherein the molybdenum- and potassium-based active component is obtained from a precursor having the formula KMoS.15. The catalyst of claim 14 , wherein the weight ratio of KMoSand Ca(PO)(OH)used to obtain the catalyst is{'br': None, 'sub': 2', '4', '10', '4', '6', '2, 'KMoS/Ca(PO)(OH)=31.3/100.'}16. The catalyst of claim 13 , wherein the molybdenum- and potassium-based active component is obtained from a precursor having structure KMoO.17. The catalyst of claim 16 , wherein the weight ratio of KMoOand Ca(PO)(OH)used to obtain the catalyst is:{'br': None, 'sub': 2', '4', '10', '4', '6', '2, 'KMoOCa(PO)(OH)=50.7/100.'}18. The catalyst of claim 11 , wherein the hydroxyapatite of the hydroxyapatite-based support has a Ca/P molar ratio ranging from 1.5 to 2.1.19. The catalyst of claim 11 , wherein the hydroxyapatite of the hydroxyapatite-based support has a Ca/P molar ratio of 1.67.20. The catalyst of claim 11 , wherein the hydroxyapatite-based support has a specific area greater than 25 m/g.21. The catalyst of claim 11 , wherein the hydroxyapatite-based support has a specific area greater than 40 m/g.22 ...

PREPARATION OF PROPANE OXIDATION CATALYSTS

A process for preparing a propane oxidation catalyst, the process comprising pre-calcining a catalyst precursor in a precalcining zone in an oxygen-containing gas, then feeding an oxygen-free gas to a purging zone until the gas exiting the zone is substantially free of oxygen, and calcining the pre-calcined precursor to obtain the catalyst. 1. A process for preparing a propane oxidation catalyst , the process comprising: (a) preparing a catalyst precursor; (b) pre-calcining the catalyst precursor in a precalcining zone in an oxygen-containing gas at a temperature of less than 330° C. to form a pre-calcined precursor; then (c) feeding an oxygen-free gas to the pre-calcined precursor in a purging zone until the gas exiting the purging zone is substantially free of oxygen , wherein the temperature of the purging zone is less than 330° C. , and (d) calcining the pre-calcined precursor to obtain the catalyst.2. The process of wherein the catalyst comprises less than 4% of MOphase.3. The process of wherein the catalyst comprises less than 2% of MOphase.4. The process of wherein the oxygen-free gas comprises primarily nitrogen.5. The process of wherein the temperature of at least one of the precalcining zone or the purging zone is less than 310° C.6. The process of . wherein the temperature of at least one of the precalcining zone or the purging zone is less than 290° C.7. The process of wherein the temperature of at least one of the precalcining zone or the purging zone is less than 280° C.8. The process of wherein step (b) is continued until the weight of the precursor stabilizes to obtain a pre-calcined precursor.9. The process of wherein the catalyst is represented by the formula AVNXZOwherein A is at least one element selected from the group consisting of Mo and W claim 1 , N is at least one element selected from the group consisting of Te and Sb claim 1 , X is at least one element selected from the group consisting of Nb claim 1 , Ta claim 1 , Ti claim 1 , Al claim 1 ...

METHOD OF INCREASING THE THICKNESS OF COLLOIDAL NANOSHEETS AND MATERIALS CONSISTING OF SAID NANOSHEETS

A process of growth in the thickness of at least one facet of a colloidal inorganic sheet. By sheet is meant a structure having at least one dimension, the thickness, of nanometric size and lateral dimensions great compared to the thickness, typically more than 5 times the thickness. By homostructured is meant a material of homogeneous composition in the thickness and by heterostructured is meant a material of heterogeneous composition in the thickness. The process allows the deposition of at least one monolayer of atoms on at least one inorganic colloidal sheet, this monolayer being constituted of atoms of the type of those contained or not in the sheet. Homostructured and heterostructured materials resulting from such process as well as the applications of the materials are also described. 1. An inorganic colloidal nanoparticle comprising an initial inorganic nanosheet partially or totally covered with at least one layer of inorganic material.2. The inorganic colloidal nanoparticle according to claim 1 , wherein the initial inorganic nanosheet is partially or totally covered on at least one of its largest faces with the at least one layer of inorganic material.3. The inorganic colloidal nanoparticle according to claim 1 , wherein the initial inorganic nanosheet is extended in the thickness with the at least one layer of inorganic material.4. The inorganic colloidal nanoparticle according to claim 1 , wherein the inorganic colloidal nanoparticle is a nanosheet.5. The inorganic colloidal nanoparticle according to claim 1 , wherein at least one part of the inorganic colloidal nanoparticle has a thickness greater than the thickness of the initial nanosheet.6. The inorganic colloidal nanoparticle according to claim 1 , wherein the inorganic colloidal nanoparticle has a thickness of 0.5 nm to 10 mm7. The inorganic colloidal nanoparticle according to claim 1 , wherein at least one lateral dimension of the inorganic colloidal nanoparticle is at least 1.5 times its ...

CATALYST FOR THE OXIDATION OF HYDROCARBONS CONSISTING OF MOLYBDENUM, VANADIUM, NIOBIUM, TELLURIUM, MANGANESE AND COBALT

A catalyst material for the oxidation and/or oxidative dehydrogenation of hydrocarbons, in particular for the selective oxidation of propane to acrylic acid, comprising a) molybdenum (Mo), b) vanadium (V), c) niobium (Nb), d) tellurium (Te), e) manganese (Mn) and cobalt, in which the molar ratio of at least one element, which is selected from manganese and cobalt, to molybdenum lies in the range 0.01 to 0.2. Furthermore, a catalyst for the oxidation and/or oxidative dehydrogenation of hydrocarbons, a use of the catalyst material or of the catalyst, a method for producing a catalyst material for the oxidation and/or oxidative dehydrogenation of hydrocarbons, and a method for the selective oxidation of propane to acrylic acid. 2. The catalyst material according to claim 1 , in which the molar ratio of at least one element claim 1 , which is selected from vanadium claim 1 , niobium and tellurium claim 1 , to molybdenum lies in the range of from 0.1:1 to 0.3:1 or 0.13:1 to 0.27:1; and/orin which nickel is contained in a molar ratio to molybdenum in the range of from 0 to 0.04.3. The catalyst material according to with an X-ray diffractogram which has diffraction reflexes h claim 1 , i claim 1 , k and l the peaks of which lie at the diffraction angles (2θ) 26.0±0.5 (h) claim 1 , 27.1±0.5 (i) claim 1 , 7.8±0.5 (k) and 28.0±0.5 (l); and/or{'sub': h', 'i', 'k', 'l', 'x (x=1 to 3), 'claim-text': [{'br': None, 'i': R', '=P', 'P', '+P, 'sub': 1', 'h', 'h', 'i, '/()>0.3; and/or'}, {'br': None, 'i': R', '=P', 'P', '+P, 'sub': 2', 'i', 'i', 'l, '/()>0.5; and/or'}, {'br': None, 'i': R', '=P', 'P', '+P, 'sub': 3', 'i', 'i', 'k, '/()<0.8; and/or'}], 'in which the intensities P, P, P, Pof the diffraction reflexes h, i, k and l satisfy the following equations, with Ras the intensity ratio defined by the equationsin which, in the X-ray diffractogram, the diffraction reflex i has the second highest intensity and/or the diffraction reflex h has the third highest intensity.4. The catalyst ...

METHOD FOR IN SITU HIGH ACTIVITY ODH CATALYST

A process for preparing an oxidative dehydrogenation catalyst or oxidative dehydrogenation catalyst precursor that includes mixing solutions of molybdenum and tellurium at a pH from about 3.3 to 7.5; adjusting the pH of the resulting solution back to about 5 and adding VOSOand adding a solution of NbOand oxalic acid and treating the resulting precursor slurry in a controlled pressure hydrothermal process to obtain the catalyst. 1. A process for preparing a catalyst comprising mixed oxides of MoVNbTe comprising the following steps:i) forming an aqueous solution of ammonium heptamolybdate (tetrahydrate) and telluric acid in a molar ratio of Mo:Te 1:0.14 to 1:0.20, at a temperature from 30° C. to 85° C. and adjusting the pH of the solution to 6.5 to 8.5, with a nitrogen-containing base to form soluble salts of the metals;ii) stirring the pH adjusted solution for a time of not less than 15 minutes;iii) adjusting the pH of the resulting solution to from 4.5 to 5.5, with an acid, and stirring the resulting solution at a temperature of 75° C. to 85° C. until it is homogeneous;iv) preparing an aqueous 0.30 to 0.50 molar solution of vanadyl sulphate at a temperature from room temperature to 80° C.;v) mixing the solutions from steps i) and iv) together to provide a molar ratio of V:Mo from 1.00:1 to 1.67:1;{'sub': 2', '2', '4', '2', '5', '2, 'vi) preparing a solution of HCOand NbOxHO in a molar ratio from 3:1:1 to 6.5:1;'}vii) adding the solution from step vi) to the solution of step v) to provide a molar ratio of Mo:Nb from 5.56:1 to 7.14:1 to form a slurry;viii) heating the resulting slurry in an autoclave under an inert gas, air, carbon dioxide, carbon monoxide and mixtures thereof at a pressure of not less than 1 psig at a temperature from 140° C. to 190° C. for not less than 6 hours.2. The process according to claim 1 , wherein the temperature for the hydrothermal treatment is from 140° C. to 180° C.3. The process according to claim 1 , wherein the pressure in the ...

AGGLOMERATED ODH CATALYST

Oxidative dehydrogenation catalysts for converting lower paraffins to alkenes such as ethane to ethylene when prepared as an agglomeration, for example extruded with supports chosen from slurries of TiO, ZrOAlO, AlO(OH) and mixtures thereof have a lower temperature at which 25% conversion is obtained. 1. An agglomerated catalyst comprising: [{'br': None, 'sub': 1.0', '0.12-0.49', '0.06-0.16', '0.15-0.20', 'd, 'MoVTeNbO'}, 'as measured by PIXE and wherein d is a number to satisfy the valence of the oxide; and, '10 wt. % to 95 wt. % of a catalyst of the formula{'sub': 2', '2', '3, '5 wt. % to 90 wt. % of a binder chosen from TiO, AlO, AlO(OH), and mixtures thereof.'}2. The agglomerated catalyst of claim 1 , having a cumulative surface area of less than 35 m/g as measured by BET.3. The agglomerated catalyst of claim 1 , having a cumulative pore volume from 0.05 to 0.50 cm/g.4. The agglomerated catalyst of claim 1 , having a pore size distribution with less than 4% having a pore width size less than 150 Angstroms.5. The agglomerated catalyst of claim 1 , wherein the agglomerated catalyst is in the shape of a sphere claim 1 , rod claim 1 , ring claim 1 , or a saddle.6. The agglomerated catalyst of claim 5 , wherein the agglomerated catalyst has an average size from 1.3 mm to 5 mm.7. The agglomerated catalyst of claim 5 , wherein the binder is an acidified binder.8. The agglomerated catalyst of claim 5 , wherein the binder is a base treated binder.9. The agglomerated catalyst of claim 7 , wherein the agglomerated catalyst is in the shape of a rod having an aspect ratio from 1 to 5/1.3 and a crush strength up to 100 N/mm.10. The agglomerated catalyst of claim 8 , wherein the agglomerated catalyst is in the shape of a rod having an aspect ratio from 1 to 5/1.3 and a crush strength up to 100 N/mm.11. The agglomerated catalyst of claim 7 , wherein the agglomerated catalyst is in the shape of a sphere having a crush strength up to 100 N.12. The agglomerated catalyst of claim 8 ...

CATALYST FOR ALKANE OXIDATIVE DEHYDROGENATION AND/OR ALKENE OXIDATION

The invention relates to a process for treating a catalyst for alkane oxidative dehydrogenation and/or alkene oxidation, which catalyst is a mixed metal oxide catalyst containing molybdenum, vanadium and niobium, wherein the process comprises: contacting the catalyst with a gas mixture comprising an inert gas and oxygen (O), wherein the amount of oxygen is of from 10 to less than 10,000 parts per million by volume (ppmv), based on the total volume of the gas mixture, at an elevated temperature. 1. A process for the oxidative dehydrogenation of ethane , comprising contacting ethane with a mixed metal oxide catalyst containing molybdenum , vanadium , tellurium and niobium under dehydrogenation conditions wherein the catalyst is pretreated by: contacting the catalyst with a gas mixture comprising an inert gas and oxygen (O) , wherein the amount of oxygen is from 250 to 10 ,000 parts per million by volume (ppmv) , based on the total volume of the gas mixture , at an elevated temperature.2. (canceled)3. A process according to claim 1 , wherein the temperature is of from 300 to 900° C.4. A process according to claim 1 , wherein the temperature is of from 400 to 800° C.5. A process according to claim 1 , wherein the temperature is of from 500 to 700° C.6. A process according to claim 1 , wherein the temperature is of from 550 to 650° C.7. A process according to claim 1 , wherein the amount of oxygen is of from 400 to 9 claim 1 ,000 parts per million by volume.8. A process according to claim 1 , wherein the amount of oxygen is of from 600 to 8 claim 1 ,500 parts per million by volume.9. A process according to claim 1 , wherein the amount of oxygen is of from 800 to 8 claim 1 ,000 parts per million by volume.10. A process according to claim 1 , wherein the amount of oxygen is of from 900 to 7 claim 1 ,500 parts per million by volume. The present application is a divisional application of U.S. patent application Ser. No. 14/398,508, filed Nov. 3, 2014 which is a National ...

PHOTOCATALYST

A photocatalyst includes a composite fiber having at least two crystalline semi-conductors that provide a heterojunction structure in the composite fiber. 1. A photocatalyst comprising a composite fiber including at least two crystalline semi-conductors , wherein the crystalline semi-conductors provide a heterojunction structure in the composite fiber.2. The photocatalyst of claim 1 , wherein the at least two crystalline semi-conductors have band position alignments which allow vectorial displacement of electrons and holes.3. The photocatalyst of claim 2 , wherein one of the crystalline semi-conductors is an n-type semi-conductor selected from the group consisting of titanium dioxide claim 2 , bismuth oxide claim 2 , zinc oxide claim 2 , and combinations thereof.4. The photocatalyst of claim 2 , wherein one of the crystalline semi-conductors is a p-type semi-conductor selected from the group consisting of copper (I) oxide claim 2 , copper (II) oxide claim 2 , cadmium telluride claim 2 , and combinations thereof.5. The photocatalyst of claim 1 , wherein one of the crystalline semi-conductors is prepared from a precursor solution including bismuth oxide in a concentration from about 0.1% to about 1% claim 1 , zinc oxide in a concentration from about 0.1% to about 1% claim 1 , and titanium dioxide in a concentration from about 1% to about 10%.6. The photocatalyst of claim 1 , wherein the composite fiber has a nanostructure.7. The photocatalyst of claim 1 , whereinthe photocatalyst is capable of removing a contaminant from a fluid stream, andthe contaminant comprises a pollutant.8. The photocatalyst of claim 1 , wherein the composite fiber further comprises a polymer coating.9. The photocatalyst of claim 1 , furthers comprising a substrate holding the composite fiber.10. The photocatalyst of claim 9 , wherein the substrate is transparent to light and is gas permeable.11. The photocatalyst of claim 9 , wherein the substrate is flexible.12. The photocatalyst of claim 9 , ...

OXIDATIVE DEHYDROGENATION OF ALKANES TO ALKENES, AND RELATED SYSTEM

A method of producing and separating an alkene, such as ethylene, from an alkane, such as ethane. The method comprises subjecting a feedstock comprising ethane to oxidative dehydrogenation to produce an ethylene stream. The ethylene stream is passed through a membrane separation unit to separate the ethylene from unreacted ethane in the ethylene stream. The ethylene is recovered from the membrane separation unit. A system configured to produce ethylene is also disclosed. The system comprises at least one ODH reactor, a heat management unit coupled to the at least one ODH reactor, and at least one membrane separation unit comprising at least one membrane. The ODH reactor is configured to convert ethane to ethylene. The heat management unit is configured to reduce a temperature of the ethylene. The at least one membrane is configured to separate the ethylene from unreacted ethane. 1. A method of producing ethylene , comprising:subjecting a feedstock comprising ethane to oxidative dehydrogenation to produce an ethylene stream;passing the ethylene stream through a membrane separation unit to separate the ethylene from unreacted ethane in the ethylene stream; andrecovering the ethylene from the membrane separation unit.2. The method of claim 1 , wherein subjecting a feedstock comprising ethane to oxidative dehydrogenation comprises subjecting the feedstock comprising the ethane and oxygen to the oxidative dehydrogenation.3. The method of claim 1 , wherein subjecting a feedstock comprising ethane to oxidative dehydrogenation comprises subjecting the feedstock comprising an excess of the ethane to the oxidative dehydrogenation.4. The method of claim 1 , wherein subjecting a feedstock comprising ethane to oxidative dehydrogenation comprises subjecting the feedstock comprising about 95% by volume of the ethane and about 5% by volume of oxygen to the oxidative dehydrogenation.5. The method of claim 1 , wherein subjecting a feedstock comprising ethane to oxidative ...

Low pressure gas release hydrothermal and peroxide treatment of odh catalyst

The preparation of an oxidative dehydrogenation catalyst comprising Mo, V, Nb and Te using a hydrothermal step. In some embodiments, the activity and reproducibility of the catalyst is improved by conducting the hydrothermal step while permitting gaseous products to leave the reactor. In some instances a condenser may be upstream of the outlet of the reactor.

ALKANE OXIDATIVE DEHYDROGENATION

The invention relates to a process of the oxidative dehydrogenation of a C2-6 alkane, comprising subjecting a stream comprising methane and the C2-6 alkane, in which stream the volume ratio of methane to the C2-6 alkane is of from 0.005:1 to 100:1, to oxydehydrogenation conditions resulting in a stream comprising methane, a C2-6 alkene and optionally a C2-6 carboxylic acid. 1. A process of the oxidative dehydrogenation of a C2-6 alkane , comprising subjecting a stream comprising methane and the C2-6 alkane , in which stream the volume ratio of methane to the C2-6 alkane is of from 0.005:1 to 100:1 , preferably of from 0.2:1 to 100:1 , more preferably of from 0.5:1 to 100:1 , to oxydehydrogenation conditions resulting in a stream comprising methane , a C2-6 alkene and optionally a C2-6 carboxylic acid.2. The process according to claim 1 , wherein the volume ratio of methane to the C2-6 alkane is of from 0.005:1 to 4.8:1.3. The process according to claim 1 , wherein C2-6 alkene is converted into another chemical product.4. The process according to claim 3 , wherein the C2-6 alkane is ethane and the C2-6 alkene is ethylene claim 3 , which ethylene is converted into ethylene oxide.5. The process according to claim 4 , comprisingsubjecting a stream comprising methane and ethane, in which stream the volume ratio of methane to ethane is of from 0.005:1 to 100:1, preferably of from 0.2:1 to 100:1, more preferably of from 0.5:1 to 100:1, to oxydehydrogenation conditions resulting in a stream comprising methane, ethylene and optionally acetic acid;subjecting ethylene and methane from the stream comprising methane, ethylene and optionally acetic acid to oxidation conditions resulting in a stream comprising ethylene oxide and methane; andrecovering ethylene oxide from the stream comprising ethylene oxide and methane. The present invention relates to a process of alkane oxidative dehydrogenation (oxydehydrogenation; ODH).It is known to oxidatively dehydrogenate alkanes, such as ...

PREPARATION OF PROPANE OXIDATION CATALYSTS

A process for preparing a propane oxidation catalyst, the process comprising pre-calcining the catalyst precursor in an oxygen-containing gas at a temperature of less than 330° C. until the weight of the precursor stabilizes to obtain a pre-calcined precursor; then calcining the pre-calcined precursor to obtain the catalyst. 1. A process for preparing a propane oxidation catalyst , the process comprising: (a) preparing a catalyst precursor; (b) pre-calcining the catalyst precursor in an oxygen-containing gas at a temperature of less than 330° C. until the weight of the precursor stabilizes to obtain a pre-calcined precursor; then (c) calcining the pre-calcined precursor to obtain the catalyst.2. The process of wherein step (b) is maintained for at least 4 hours.3. The process of wherein step (c) is maintained for at least 6 hours.4. The process of wherein step (c) is maintained for at least 8 hours.5. The process of claim 1 , wherein the amount of phase M2 in the catalyst is less than 12%.6. The process of claim 1 , wherein the amount of phase M2 in the catalyst is less than 10%.7. The process of claim 1 , wherein the amount of phase M2 in the catalyst is less than 8%.8. The process of claim 1 , wherein the amount of phase M2 in the catalyst is less than 7%.9. The process of claim 1 , wherein the temperature of step (b) is less than 310° C.10. The process of claim 1 , wherein the catalyst is represented by the formula AaVbNcXdZeOf wherein A is at least one element selected from the group consisting of Mo and W claim 1 , N is at least one element selected from the group consisting of Te and Sb claim 1 , X is at least one element selected from the group consisting of Nb claim 1 , Ta claim 1 , Ti claim 1 , Al claim 1 , Zr claim 1 , Cr claim 1 , Mn claim 1 , Fe claim 1 , Ru claim 1 , Co claim 1 , Rh claim 1 , Ni claim 1 , Pt claim 1 , Sb claim 1 , Bi claim 1 , B claim 1 , In claim 1 , As claim 1 , Ge claim 1 , Sn claim 1 , Hf claim 1 , Pb claim 1 , P claim 1 , Pm claim ...

FACILITATED CO2 TRANSPORT MEMBRANE AND METHOD FOR PRODUCING SAME, AND METHOD AND APPARATUS FOR SEPARATING CO2

Provided is a facilitated COtransport membrane having an improved COpermeance and an improved CO/Hselectivity. The facilitated COtransport membrane includes a separation-functional membrane that includes a hydrophilic polymer gel membrane containing a COcarrier and a COhydration catalyst. Further preferably, the COhydration catalyst at least has catalytic activity at a temperature of 100° C. or higher, has a melting point of 200° C. or higher, or is soluble in water. 1. A method for separating COusing a facilitated COtransport membrane , the facilitated COtransport membrane comprising a separation-functional membrane that includes a hydrophilic polymer gel membrane containing a COcarrier with a COhydration catalyst having catalytic activity at a temperature of 100° C. or higher ,{'sub': 2', '2', '2', '2', '2', '2, 'wherein a mixed gas containing COand Hand having a temperature of 100° C. or higher is supplied to a supply side of the facilitated COtransport membrane under a condition that a pressure difference between the supply side and a permeate side of the facilitated COtransport membrane is not less than 200 kPa, and the COpassing through the facilitated COtransport membrane is separated from the mixed gas, and'}{'sub': '2', 'wherein the COhydration catalyst contains at least one of a tellurous acid compound, a selenious acid compound, an orthosilicic acid compound and a molybdic acid compound.'}2. The method of claim 1 , wherein the gel membrane is a hydrogel.3. The method of claim 1 , wherein the gel membrane is a polyvinyl alcohol-polyacrylic acid salt copolymer gel membrane.4. The method of claim 1 , wherein the COcarrier contains at least one of a carbonate of an alkali metal claim 1 , a bicarbonate of an alkali metal and a hydroxide of an alkali metal.5. The method of claim 4 , wherein the alkali metal is cesium or rubidium.6. The method of claim 1 , wherein the separation-functional membrane is supported on a hydrophilic porous membrane.7. A COseparation ...

HEAT DISSIPATING DILUENT IN FIXED BED REACTORS

Incorporating into a fixed bed reactor for an exothermal reaction having a catalyst supported on a support having a thermal conductivity typically less than 30 W/mk within the reaction temperature control limits heat dissipative particles having a thermal conductivity of at least 50 W/mk less than 30 W/mk within the reaction temperature control limits helps control the temperature of the reactor bed. 117-. (canceled)18. A process for conducting an oxidative dehydrogenation of one or more Chydrocarbons comprising{'sub': '2-4', 'sup': '−1', 'claim-text': {'br': None, 'sub': x', 'y', 'z', 'm', 'n', 'p, 'VMoNbTeMeO'}, 'providing a mixed feed of Chydrocarbons and oxygen in a volume ratio from 70:30 to 95:5 to a fixed bed reactor at a temperature of less than 420° C., a gas hourly space velocity of not less than 280 hrand a pressure of from 0.8 to 102 atmospheres (80 to 1000 kPa) in the presence of a fixed bed comprising a mixed metal oxide catalyst having the empirical formulawherein Me is a metal selected from Ta, Ti, W, Hf, Zr, Sb and mixtures thereof; x is from 0.1 to 3 provided that when Me is absent x is greater than 0.5; y is from 0.5 to 1.5; z is from 0.001 to 3; m is from 0.001 to 5; n is from 0 to 2; and p is a number to satisfy the valence state of the mixed metal oxide catalyst;wherein said mixed metal oxide catalyst is supported on one or more of porous silicon dioxide, ignited silicon dioxide, kieselgur, silica gel, porous or nonporous aluminum oxide, titanium dioxide, zirconium dioxide, thorium dioxide, lanthanum oxide, magnesium oxide, calcium oxide, barium oxide, tin oxide, cerium dioxide, zinc oxide, boron oxide, boron nitride, boron carbide, boron phosphate, zirconium phosphate, aluminum silicate, silicon nitride or silicon carbide;wherein said fixed bed further comprises one or more inert non catalytic heat dissipative particles in an amount from 5 to 90 wt. %, based on the weight of the fixed bed;wherein, said particles have a melting point at least ...

Heat dissipating diluent in fixed bed reactors

Incorporating into a fixed bed reactor for an exothermal reaction having a catalyst supported on a support having a thermal conductivity typically less than 30 W/mk within the reaction temperature control limits heat dissipative particles having a thermal conductivity of at least 50 W/mk less than 30 W/mk within the reaction temperature control limits helps control the temperature of the reactor bed.

Oxidative dehydrogenation (odh) of ethane

Processes and associated reaction systems for the oxidative dehydrogenation of ethane are provided. In particular, a process is provided that comprises supplying a feed gas comprising ethane and oxygen to a multitubular fixed-bed reactor and allowing the ethane and oxygen to react in the presence of an oxidative dehydrogenation catalyst to yield a reactor effluent comprising ethylene; and supplying a coolant to an interior shell space of the multitubular fixed-bed reactor in a flow pattern that is co-current with the flow of the feed gas through reactor.

Oxidative dehydrogenation catalyst

Oxidative dehydrogenation catalysts comprising MoVNbTeO having improved consistency of composition and a 25% conversion of ethylene at less than 420° C. and a selectivity to ethylene above 95% are prepared by treating the catalyst precursor with H 2 O 2 in an amount equivalent to 0.30-2.8 mL H 2 O 2 of a 30% solution per gram of catalyst precursor prior to calcining.

OXIDATIVE DEHYDROGENATION CATALYST

Oxidative dehydrogenation catalysts comprising MoVNbTeO having improved consistency of composition and a 25% conversion of ethylene at less than 420° C. and a selectivity to ethylene above 95% are prepared by treating the catalyst precursor with HOin an amount equivalent to 0.30-2.8 mL HOof a 30% solution per gram of catalyst precursor prior to calcining. 1. A method for the oxidative dehydrogenation of a mixed feed comprising ethane and oxygen in a volume ratio from 70:30 to 95:5 , wherein the method comprises passing the mixed feed over a calcined oxidative dehydrogenation catalyst of the empirical formula:{'br': None, 'sub': 1.0', '0.22-0.33', '0.10-0.16', '0.15-0.19', 'd, 'MoVTeNbO'}wherein d is a number to satisfy the valence of the oxide and the empirical formula is determined by PIXE; and{'sub': 2', '2, 'wherein the calcined oxidative dehydrogenation catalyst is formed from a catalyst precursor that is treated with HOand wherein the catalyst precursor is calcined at a temperature from 200° C. to 600° C.'}2. The method of claim 1 , wherein the gas hourly space velocity greater than 3000 hr..3. The method of claim 1 , wherein the temperature is less than 400° C.4. The method of claim 1 , wherein the calcined oxidative dehydrogenation catalyst forms a fixed bed in the reactor.5. The method of claim 1 , wherein the gas hourly space velocity is not less than 3000 hr claim 1 , the calcined oxidative dehydrogenation catalyst forms a fixed bed in the reactor claim 1 , and the selectivity to ethylene is not less than 90%.6. The method according to claim 1 , wherein the calcined oxidative dehydrogenation catalyst has the empirical formula:{'br': None, 'sub': 1.0', '0.22-0.29', '0.10-0.16', '0.15-0.19', 'd, 'MoVTeNbO'}wherein d is a number to satisfy the valence of the oxide and the empirical formula is determined by PIXE.7. The method according to claim 1 , wherein the calcined oxidative dehydrogenation catalyst has the empirical formula:{'br': None, 'sub': 1.0', '0.22 ...

ALKANE OXIDATIVE DEHYDROGENATION AND/OR ALKENE OXIDATION

The invention relates to a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms, wherein a gas stream comprising oxygen and the alkane and/or alkene is contacted with a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium, and wherein the weight hourly space velocity is of from 2.1 to 25.0 hrand the temperature is of from 300 to 500° C. 1. Process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms , wherein a gas stream comprising oxygen and the alkane and/or alkene is contacted with a mixed metal oxide catalyst containing molybdenum , vanadium , niobium and optionally tellurium , and wherein the weight hourly space velocity is of from 2.1 to 25.0 hrand the temperature is of from 300 to 500° C.2. Process according to claim 1 , wherein the weight hourly space velocity is of from 4.0 to 18.0 hr.3. Process according to claim 1 , wherein the temperature is of from 310 to 450° C.4. Process according to claim 1 , wherein the pressure is of from 0.1 to 15 bara.5. Process according to claim 1 , wherein the process is a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and wherein said alkane is ethane or propane.6. Process according to claim 1 , wherein the process is a process of the oxidation of an alkene containing 2 to 6 carbon atoms and wherein said alkene is ethylene or propylene. The present invention relates to a process of alkane oxidative dehydrogenation (oxydehydrogenation; ODH) and/or alkene oxidation.It is known to oxidatively dehydrogenate alkanes, such as alkanes containing 2 to 6 carbon atoms, for example ethane or propane resulting in ethylene and propylene, respectively, in an oxidative dehydrogenation (oxydehydrogenation; ODH) process. Examples of alkane ODH processes, including catalysts and ...

ALKANE OXIDATIVE DEHYDROGENATION AND/OR ALKENE OXIDATION

The invention relates to a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms, wherein a gas stream comprising oxygen and the alkane and/or alkene is contacted with a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium, and wherein the linear velocity of said gas stream is at least 10 cm/sec. 1. Process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms , wherein a gas stream comprising oxygen and the alkane and/or alkene is contacted with a mixed metal oxide catalyst containing molybdenum , vanadium , niobium and optionally tellurium , and wherein the linear velocity of said gas stream is at least 10 cm/sec.2. Process according to claim 1 , wherein the linear velocity of the gas stream comprising oxygen and the alkane and/or alkene is in the range of from 10 to 500 cm/sec.3. Process according to claim 1 , wherein the gas hourly space velocity is of from 2 claim 1 ,500 to 25 claim 1 ,000 hr.4. Process according to claim 1 , wherein the pressure is of from 0.1 to 15 bara.5. Process according to claim 1 , wherein the temperature is of from 300 to 500° C.6. Process according to claim 1 , wherein the process is a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and wherein said alkane is ethane or propane.7. Process according to claim 1 , wherein the process is a process of the oxidation of an alkene containing 2 to 6 carbon atoms and wherein said alkene is ethylene or propylene. The present invention relates to a process of alkane oxidative dehydrogenation (oxydehydrogenation; ODH) and/or alkene oxidation.It is known to oxidatively dehydrogenate alkanes, such as alkanes containing 2 to 6 carbon atoms, for example ethane or propane resulting in ethylene and propylene, respectively, in an oxidative ...

METHOD AND APPARATUS FOR MANUFACTURING CONTINUOUS ACRYLIC ACID THROUGH PROPANE PARTIAL OXIDATION REACTION

This invention relates to a method of continuously preparing acrylic acid and an apparatus using the same, the method including: (1) subjecting a feed including propane, oxygen, water vapor and carbon dioxide to partial oxidation using a catalyst, thus obtaining an acrylic acid-containing mixed gas, (2) separating the acrylic acid-containing mixed gas into an acrylic acid-containing solution and a gas byproduct, (3) separating an acrylic acid solution from the separated acrylic acid-containing solution, and (4) recycling the separated gas byproduct into the feed. 1. A method of continuously preparing acrylic acid , comprising steps of:(1) subjecting a feed including propane, oxygen, water vapor and carbon dioxide to partial oxidation using a catalyst, thus obtaining an acrylic acid-containing mixed gas;(2) separating the acrylic acid-containing mixed gas into an acrylic acid-containing solution and a gas byproduct;(3) separating an acrylic acid solution from the separated acrylic acid-containing solution; and(4) recycling the separated gas byproduct into the feed.2. The method of claim 1 , wherein the gas byproduct includes at least one selected from the group consisting of propane claim 1 , propylene claim 1 , oxygen claim 1 , carbon monoxide claim 1 , carbon dioxide claim 1 , and water vapor.3. The method of claim 1 , wherein the separated gas byproduct of the step (4) is recycled so as to be suitable for a composition molar ratio of the feed in the step (1).4. The method of claim 1 , further comprising oxidizing carbon monoxide into carbon dioxide using a catalyst including at least one selected from the group consisting of rhodium (Rh) claim 1 , iridium (Ir) claim 1 , palladium (Pd) claim 1 , and platinum (Pt) claim 1 , between the steps (1) and (2).5. The method of claim 1 , further comprising oxidizing carbon monoxide into carbon dioxide using a catalyst including at least one selected from the group consisting of rhodium (Rh) claim 1 , iridium (Ir) claim 1 , ...

PHOTOCATALYST

A photocatalyst includes a composite fiber having at least two crystalline semi-conductors that provide a heterojunction structure in the composite fiber. 115-. (canceled)16. A device for removing a contaminant from a fluid stream , the device comprising a photocatalyst including a composite fiber , whereinthe composite fiber includes at least three n-type crystalline semiconductor materials,the n-type crystalline semiconductor materials form a heterojunction structure in the composite fiber, andthe n-type crystalline semiconductor materials include bismuth oxide, titanium dioxide, and zinc oxide.17. The device of claim 16 , wherein the photocatalyst is activated by light incident on the photocatalyst and selected from the group consisting of ultra-violet light claim 16 , visible light claim 16 , and combinations of ultra-violet light and visible light.18. The device of claim 16 , including a filter located upstream of the photocatalyst in the device.19. The device of claim 16 , wherein the photocatalyst has a pleated configuration.20. The device of claim 16 , wherein the photocatalyst protrudes into the fluid stream from an internal wall of the device.21. A method comprising: the photocatalyst comprises a composite fiber,', 'the composite fiber includes at least three n-type crystalline semiconductor materials,', 'the n-type crystalline semiconductor materials form a heterojunction structure in the composite fiber, and', 'the n-type crystalline semiconductor materials include bismuth oxide, titanium dioxide, and zinc oxide; and, 'placing a device including a photocatalyst adjacent a fluid stream, wherein'}activating the photocatalyst, for photocatalytic reaction, with light incident on the photocatalyst for removing a contaminant from the fluid stream.22. The method of claim 21 , wherein the photocatalyst includes a substrate holding the composite fiber therein.23. The method of claim 21 , wherein the photocatalyst is positioned substantially tangentially with ...

SYNTHESIS OF A MOVTENB CATALYST FROM LOW-COST METAL OXIDES

A novel catalyst and process for producing a mixed oxide material containing molybdenum, vanadium, tellurium and niobium is disclosed. The material can be used as a catalyst for the oxidative dehydrogenation of ethane to ethene or the oxidation of propane to acrylic acid.

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

The invention relates to a catalyst comprising an active component based on molybdenum and on potassium and a support based on hydroxyapatite, and also to a process for preparing said catalyst and a process for producing methyl mercaptan in a catalytic process by reaction of carbon monoxide, sulphur and/or hydrogen sulphide and hydrogen, comprising the use of said catalyst. 1. A catalyst comprising a molybdenum- and potassium-based active component and a hydroxyapatite-based support.2. The catalyst as claimed in claim 1 , wherein the catalyst support is hydroxyapatite having stoichiometric formula Ca(PO)(OH).3. The catalyst as claimed in claim 1 , wherein the molybdenum- and potassium-based active component is selected from the group consisting of compounds based on Mo—S—K claim 1 , compounds based on Mo—O—K claim 1 , and their mixtures.4. The catalyst as claimed in claim 3 , wherein the molybdenum- and potassium-based active component has been obtained from a precursor having structure KMoS.5. The catalyst as claimed in claim 4 , wherein the weight ratio of KMoSand Ca(PO)(OH)used to obtain the catalyst is{'br': None, 'sub': 2', '4', '10', '4', '6', '2, 'KMoS/Ca(PO)(OH)=31.3/100'}6. The catalyst as claimed in claim 3 , wherein the molybdenum- and potassium-based active component has been obtained from a precursor having structure KMoO.7. The catalyst as claimed in claim 6 , wherein the weight ratio of KMoOand Ca(PO)(OH)used to obtain the catalyst is:{'br': None, 'sub': 2', '4', '10', '4', '6', '2, 'KMoO/Ca(PO)(OH)=50.7/100'}8. A preparation process for the catalyst as defined in claim 1 , comprising the following steps:preparing a precursor for the molybdenum- and potassium-based active component;preparing the hydroxyapatite-based support; anddry impregnating the hydroxyapatite-based support with the precursor for the molybdenum- and potassium-based active component.9. A process for producing methyl mercaptan in a catalytic process by reacting carbon oxide claim 1 , ...

CATALYST FOR ETHANE ODH

A catalyst for oxidative dehydrogenation (ODH) of ethane with an empirical formula Mo—V—Te—Nb—Pd—O produced using a process comprising impregnation of the Pd component on the surface of the catalyst following a calcination step using a Pd compound free of halogens. The resulting catalyst can be used in both diluted and undiluted ODH processes and shows higher than expected activity without any loss of selectivity. 2. The process of wherein the step ii) heating of said first mixture in said first pressurized vessel is done at a temperature of from 160° C. to 185° C.3. The process of wherein the step vi) drying temperature is from 120° C. to 130° C.4. The process of wherein b equals from 0.1 to 0.5.5. The process of wherein b equals from 0.2 to 0.4.6. The process of wherein c equals from 0.05 to 0.4.7. The process of wherein c equals from 0.08 to 0.3.8. The process of wherein d equals from 0.05 to 0.4.9. The process of wherein d equals from 0.08 to 0.3.10. The process of wherein d equals from 0.10 to 0.25.11. The process of wherein e equals from 0.005 to 0.10.12. The process of wherein e equals from 0.01 to 0.05.13. The process of wherein e equals from 0.015 to 0.03.14. The process of wherein the inert atmosphere comprises gaseous nitrogen.15. The process of wherein the said first recovered insoluble material is calcined at a temperature of from 500° C. to 700° C. claim 1 , (preferably from 550° C. to 650° C. claim 1 , most preferably from 580° C. to 620° C.) claim 1 , for from 1 hours to 8 hours.16. The process of wherein the said first recovered insoluble material is calcined by ramping temperature from at or about room temperature to at or about 600° C. over a period of 4 to 7 hours claim 1 , followed by holding at or about 600° C. for from 1 hour to 4 hours.17. The process of wherein the Pd compound free of halogens is selected from [Pd(NH)](NO) claim 1 , Pd(HCO) claim 1 , Pd(CHCOO)and an analogous Pd containing salt.18. The process of wherein impregnation of said ...

METHOD FOR PRODUCING MIXED OXIDE MATERIALS CONTAINING MOLYBDENUM

The invention relates to a method for producing a mixed oxide material containing the elements molybdenum, vanadium, niobium and tellurium, comprising the following steps: a) producing a mixture from starting compounds containing molybdenum, vanadium, niobium and a tellurium-containing starting compound, present in the tellurium in the +4 oxidation state, b) hydrothermal treatment of the mixture from starting compounds at a temperature of between 100° C. to 300° C., in order to obtain a product suspension, c) separating off and drying the solid material from the product suspension obtained in step b), d) activating the solid material in inert gas in order to obtain the mixed oxide material. The invention is characterized in that the tellurium-containing starting compound has a particle size Dof less than 100 μm. 1. A method for preparing a mixed-oxide material containing the elements molybdenum , vanadium , niobium , and tellurium , comprising the following steps:a) preparation of a mixture of starting compounds that contains molybdenum, vanadium, niobium, and a tellurium-containing starting compound in which tellurium is in oxidation state +4,b) hydrothermal treatment of the mixture of starting compounds at a temperature of 100° C. to 300° C. to obtain a product suspension,c) separation and drying of the solid from the product suspension resulting from step b),{'sub': '90', 'd) activation of the solid in inert gas to obtain the mixed-oxide material, characterized in that the tellurium-containing starting compound has a particle size Dsmaller than 100 μm.'}2. The method as claimed in claim 1 , wherein the mixture of starting compounds is an aqueous suspension.3. The method as claimed in claim 1 , wherein the tellurium-containing starting compound is tellurium dioxide or a compound of formula MTeOwhere n=1 or 2 and x=2/n and wherein M is an alkali metal or alkaline earth metal.4. The method as claimed in claim 1 , wherein one of the starting compounds is ammonium ...

DOUBLE PEROXIDE TREATMENT OF OXIDATIVE DEHYDROGENATION CATALYST

Oxidative dehydrogenation catalysts comprising MoVNbTeO having improved consistency of composition and a 25% conversion of ethylene at less than 420° C. and a selectivity to ethylene above 95% are prepared by treating the catalyst precursor with HOin an amount equivalent to 0.30-2.8 mL HOof a 30% solution per gram of catalyst precursor prior to calcining and treating the resulting catalyst with the equivalent amount of peroxide after calcining. 114-. (canceled)151. A method for the oxidative dehydrogenation of a mixed feed of ethane and oxygen in a volume ratio from 70:30 to 95:5 at a temperature less than 400° C. , at a gas hourly space velocity of not less than 280 hrand a pressure from 0.8 to 1.2 atmospheres comprising passing said mixture over a catalyst prepared according to claim .16. The method according to claim 15 , wherein the selectivity to ethylene is not less than 90%.17. The method according to claim 16 , wherein the gas hourly space velocity is not less than 1000 hr.18. The method according to claim 17 , wherein the calcined catalyst forms a fixed bed in the reactor.20. The catalyst according to claim 19 , wherein not less than 75 wt % of a crystalline component has the formula (TeO)(MoVNb)Oas determined by XRD.21. The catalyst according to claim 19 , wherein from 2.4 to 12 wt % of the crystalline phase of the catalyst has the formula (TeO)(MoVNb)Oas determined by XRD.22. The catalyst according to claim 19 , wherein in the crystalline phase of the catalyst the amount of the phase having the formula (TeO)(MoVNb)Ois above 75 wt % of the measured crystalline phase.23. The catalyst according to claim 19 , has an XRD pattern (reflections data) where the reflection at 21.81° (±0.4°) 2θ is 1-6% relative peak height of the reference reflection at 22.29° (±0.4°) 2θ.24. The catalyst according to claim 19 , wherein the reflection at 22.29° (±0.4°) 2θ has a full width at half maximum (FWHM) less than 0.185° 2θ.25. The catalyst according to claim 19 , having a ...

Activated multimetal oxide catalyst

Process for producing molybdenum-containing metal oxide fluid-bed catalyst

A process for producing a molybdenum-containing metal oxide fluid-bed catalyst comprising, as essential components, (i) at least one element selected from the group consisting of iron, bismuth, and tellurium, (ii) molybdenum, and (iii) silica, which comprises (a) adjusting an aqueous slurry containing a raw material providing element (i), a molybdenum compound, a silica sol, and a chelating agent capable of inhibiting gelation of the slurry of a pH of at least 6, or (b) adjusting an aqueous slurry containing a raw material providing element (i), a molybdenum compound and a chelating agent capable of inhibiting gelation to a pH of at least 6 and mixing the slurry with a silica sol, then spray drying the thus pH-adjusted aqueous slurry, and calcining the resulting particles.

Process for production of attrition resistant antimony oxide containing fluidized bed catalyst having controlled particle size distribution

A process for producing an attrition resistant antimony oxide containing fluidized bed catalyst comprising particles within a controlled particle size distribution comprising: (a) preparing a slurry containing a pentavalent antimony compound, one or more polyvalent metal compounds and a silica sol as essential components; (b) adjusting the pH of the above slurry to not more than 7 and heating the slurry at a temperature of from about 40° C to about 150° C for at least 20 minutes while keeping the mixture in a slurry state to form a slurry containing pentavalent antimony; (c) spray-drying the thus obtained slurry to form substantially spherical particles; (d) separating extremely fine particles and/or coarse particles unsuitable for practical use from the above obtained particles and returning these separated particles to the slurry prior to the spray-drying in step (c) as they are or after the pulverization thereof; and (e) calcining the particles from which the extremely fine particles and/or coarse particles have been removed at a temperature of from about 400° C to about 1100° C.

Mixed oxide catalysts for catalytic gas phase oxidation

The invention relates to mixed oxide catalysts for the catalytic gas phase oxidation of alkanes, or mixtures of alkanes and olefins, for the production of aldehydes and carboxylic acids with air or oxygen in the presence of inert gases at elevated temperatures and pressure, and a method for the production of catalysts.

Preparation of a multimetal oxide material

A process for preparing a multimetal oxide material which contains the elements Mo, V and Te and/or Sb and at least one of the elements Nb, Ti, W, Ta and Ce and if desired promoters and has a specific X-ray diffraction pattern, in which process the last process step comprises washing with acidic liquids. In addition, a multimetal oxide material obtainable in such a way is used as a catalyst for heterogeneously catalyzed gas-phase partial oxidations and/or ammoxidation of hydrocarbons.

Heat dissipating diluent in fixed bed reactors

Incorporating into a fixed bed reactor for an exothermal reaction having a catalyst supported on a support having a thermal conductivity typically less than 30 W/mk within the reaction temperature control limits heat dissipative particles having a thermal conductivity of at least 50 W/mk less than 30 W/mk within the reaction temperature control limits helps control the temperature of the reactor bed.

Heat dissipating diluent in fixed bed reactors

Incorporating into a fixed bed reactor for an exothermal reaction having a catalyst supported on a support having a thermal conductivity typically less than 30 W/mk within the reaction temperature control limits heat dissipative particles having a thermal conductivity of at least 50 W/mk less than 30 W/mk within the reaction temperature control limits helps control the temperature of the reactor bed.

Heat dissipating diluent in fixed bed reactors

Incorporating into a fixed bed reactor for an exothermal reaction having a catalyst supported on a support having a thermal conductivity typically less than 30 W/mk within the reaction temperature control limits heat dissipative particles having a thermal conductivity of at least 50 W/mk less than 30 W/mk within the reaction temperature control limits helps control the temperature of the reactor bed.

Heat dissipating diluent in fixed bed reactors

Incorporating into a fixed bed reactor for an exothermal reaction having a catalyst supported on a support having a thermal conductivity typically less than 30 W/mk within the reaction temperature control limits heat dissipative particles having a thermal conductivity of at least 50 W/mk less than 30 W/mk within the reaction temperature control limits helps control the temperature of the reactor bed.

SOLID COMPOSITIONS AND PROPAN OR ISOBUTAN CATALYTIC CONVERSION PROCESS

Polymerization using a selenium or tellurium treated catalyst

A process comprising treating silica with at least one of selenium or tellurium under nonoxidizing conditions at a temperature of at least 370 DEG C. and a subsequent second step wherein the thus-treated silica is contacted with an oxidizing ambient at a temperature within the range of 370 DEG -900 DEG C. The silica can contain a chromium compound in which case the resulting product is suitable as a catalyst for the production of higher melt flow olefin polymers suitable for such applications as injection molding, and the like requiring a relatively narrow molecular weight distribution.

METHOD FOR PRODUCING METHACROLEIN AND METHACRYLIC ACID

Werkwijze voor het bereiden van acrylonitril en werkwijze voor het vervaardigen van een katalysator geschikt voor toepassing bij voornoemde werkwijze.

Mo and V-containing multimetal oxide materials

Multimetalloxidmasse der allgemeinen Formel I Aa[Mo5-b-cVbXcOd]1 (I),mit A = wenigstens eines der Elemente aus der Gruppe umfassend NH4, Na, K, Rb, Cs und Tl; X = eines oder mehrere der Elemente aus der Gruppe umfassend La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, Ti, Zr, Hf, Nb, Ta, W, Mn, Re, Fe, Co, Ni, Cr, Ru, Rh, Pd, Os, Ir, Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, C, Si, Ge, Sn, Pb, P, As, Sb, Bi, S, Se und Te; a = 0,1 bis 1; b = 0,25 bis 4,5; und c = 0 bis 4,5, mit der Maßgabe, dass b + c ≤ 4,5, deren Röntgendiffraktogramm das nachfolgende Röntgenbeugungsmuster RM, wiedergegeben in Gestalt von von der Wellenlänge der verwendeten Röntgenstrahlung unabhängigen Netzebenenabständen d [Å], d [Å] 3,06 ± 0,2... Multimetal oxide material of the general formula I Aa [Mo5-b-cVbXcOd] 1 (I), with A = at least one of the elements from the group comprising NH4, Na, K, Rb, Cs and Tl; X = one or more of the elements from the group comprising La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, Ti, Zr, Hf, Nb, Ta , W, Mn, Re, Fe, Co, Ni, Cr, Ru, Rh, Pd, Os, Ir, Pt, Cu, Ag, Au, Zn, Cd, Hg, B, Al, Ga, In, C, Si , Ge, Sn, Pb, P, As, Sb, Bi, S, Se and Te; a = 0.1 to 1; b = 0.25 to 4.5; and c = 0 to 4.5, with the proviso that b + c ≤ 4.5, the X-ray diffraction pattern of which is the following X-ray diffraction pattern RM, reproduced in the form of lattice plane spacings d [Å], d [Å] that are independent of the wavelength of the X-ray radiation used 3.06 ± 0.2 ...

Sequential production of a library of solids (especially heterogeneous catalysts) comprises dosing solutions, emulsions and/or dispersions into a mixer and drying, with variations and repetition

Sequential production of a library of N different solids (especially heterogeneous catalysts) whereby N reaches an integer >= 2 in one day involves dosing solutions, emulsions and/or dispersions into a mixer and drying the mixture, the ratios in the dosing step being varied and the dosing, drying and variation steps being repeated N-1 times. Sequential production of a library of N different solids (especially heterogeneous catalysts) whereby N reaches an integer >= 2 in one day involves (a) production of (i) >= 2 different sprayable solutions, emulsions and/or dispersions of elements and/or compounds providing chemical elements as solids and optionally (ii) inorganic carrier dispersions; (b) continually dosing the solutions etc. in predetermined ratios into a mixer to give homogeneous mixing; (c) continuously drying the mixture and removing it from the mixer; (d) varying the ratios in step (b) and repeating the steps (b), (c) and (d) N-1 times to recover N different dry mixtures; and (e) optionally forming and optionally calcining the mixtures to yield solids. Independent claims are also included for (1) an apparatus for the sequential production comprising >= 2 vessels for the solutions etc., a mixer, pumps and interconnecting tubes for the vessels and the mixer, a dryer connected to the mixer, and a central computer controlling the pumps and (2) parallel testing of the solids library for desired catalytic properties by separately introducing the individual solids into multi-reactors and then testing them.

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Твердая композиция с каталитической активностью (варианты) и способ окислительного аммонолиза низших алканов с ее применением

1. Твердая композиция с каталитической активностью в газофазном окислительном аммонолизе или окислении пропана и изобутана, которую получают способом, включающим: ! получение предшественника катализатора в виде сухих частиц, содержащего элементы: молибден (Mo), ванадий (V), по меньшей мере один другой элемент, способный образовать положительные ионы и повысить каталитическую активность композиции в газофазном окислительном аммонолизе пропана и/или изобутана; ! прокаливание предшественника катализатора в условиях, выбранных таким образом, чтобы в полученном основном катализаторе образовалась по меньшей мере одна кристаллическая фаза, активная в газофазном окислительном аммонолизе или окислении пропана и изобутана; ! пропитку основного катализатора водной средой, содержащей источники одного или нескольких элементов, который выбирают из группы, состоящей из сурьмы (Sb), церия (Ce), ниобия (Nb), теллура (Te) и титана (Ti), и затем сушку полученного вещества; и ! термообработку высушенного вещества в атмосфере газа, практически не содержащего кислорода, при температуре по меньшей мере 400°C с образованием смешанной металлоксидной композиции с повышенной каталитической активностью в газофазном окислительном аммонолизе или окислении пропана и изобутана по сравнению с основным катализатором. ! 2. Композиция по п.1, в которой смешанный оксид металла содержит в качестве компонентов элементы: молибден (Мо), ванадий (V) и по меньшей мере один элемент, который выбирают из группы, состоящей из сурьмы (Sb), теллура (Te) и ниобия (Nb). ! 3. Композиция по п.1, в которой смешанный оксид металла содержит по меньшей мере первую кристаллическую � РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2009 140 375 (13) A (51) МПК B01J 23/28 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2009140375/04, 01.04.2008 (71) Заявитель(и): ИНЕОС ЮЭсЭй ЭлЭлСи (US) Приоритет(ы): (30) Конвенционный приоритет: 03.04.2007 US 11/732,213 ...

制造乙烯和乙酸的方法

一种方法，其包括在氧存在下，在450℃或更低的温度下，在气相中将乙烷催化转化为乙烯和乙酸，其中所述催化剂具有经验式MoV a Nb b Te c Z d O n 。

IR And/Or SM Promoted Multi-Metal Oxide Catalyst

증진된 혼합 금속 산화물을 포함하는 촉매는 불포화 카르복시산으로 알칸 혹은 알칸과 알켄 혼합물를 기상산화시키는 경우 및 불포화 니트릴로 알칸 혹은 알칸과 알켄 혼합물을 기상 가암모니아산화반응 시키는 경우에 유용하다. Catalysts comprising enhanced mixed metal oxides are useful for the gas phase oxidation of alkanes or alkanes and alkenes with unsaturated carboxylic acids and for the gas phase ammonia oxidation of alkanes or alkanes and alkenes with unsaturated nitriles. 증진된 혼합 금속 산화물, 기상산화 Enhanced mixed metal oxides, gas phase oxidation

Method of producing unsaturated carboxylic acid from alkane

FIELD: chemistry. ^ SUBSTANCE: invention relates to a single-step method for vapour-phase oxidation of an alkane such as propane which leads to production of unsaturated caboxylic acid such as acrylic or methacrylic acid in the presence of a mixed metal oxide catalyst and excess alkane with respect to amount of oxygen. The method of producing unsaturated carboxylic acid involves: (a) reacting alkane and oxygen-containing gas in a reaction zone with a catalyst which contains mixed metal oxide under conditions which enable production of a gaseous product containing unsaturated carboxylic acid, unreacted alkane and an alkene by-product; (b) extraction of unreacted alkane and alkene by-product from the gaseous product; and (c) recycling the mixture of the extracted unreacted alkane and alkene by-product to the reaction zone without separating components; in which the mixed metal oxide consists of material with general formula MoVvAaBbCcOx where Mo is molybdenum, V is vanadium, each of A, B and C represents niobium, antimony, tellurium, silver, tantalum, titanium, aluminium, zirconium, chromium, manganese, iron, ruthenium, cobalt, rhodium, nickel, platinum, bismuth, boron, indium, arsenic, germanium, tin, lithium, sodium, potassium, rubidium, caesium, francium, beryllium, magnesium, calcium, stronium, barium, hafnium, lead, phosphorus, promethium, europium, gadolinium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, gold, selenium, palladium, gallium, zinc, praseodymium, rhenium, iridium, neodymium, yttrium, samarium and terbium, v equals 0.1-0.5, a equals 0.01-0.2, b equals 0.0-0.5, c equals 0.0-0.5, value of x is determined by valency of other components, in which alkane is propane or isobutane; where the alkane is in excess relative oxygen and molar ratio alkane: oxygen ranges from 3:1 to 1:1; and in which amount of alkene recycled to the reactor corresponds to the molar ratio alkane: alkene equal to 1:0.03-1:0.1. ^ EFFECT: improved method. ^ 14 cl, 3 tbl, ...

Promoted Multi-Metal Oxide Catalyst

증진된 혼합 금속 산화물을 포함하는 촉매는 불포화 카르복시산으로 알칸 혹은 알칸과 알켄 혼합물를 기상산화시키는 경우 및 불포화 니트릴로 알칸 혹은 알칸과 알켄 혼합물을 기상 가암모니아산화반응 시키는 경우에 유용하다. Catalysts comprising enhanced mixed metal oxides are useful for the gas phase oxidation of alkanes or alkanes and alkenes with unsaturated carboxylic acids and for the gas phase ammonia oxidation of alkanes or alkanes and alkenes with unsaturated nitriles. 증진된 혼합 금속 산화물, 기상산화 Enhanced mixed metal oxides, gas phase oxidation

Process for making ethylene and acetic acid

본 발명은 산소의 존재하에 450℃ 이하의 온도에서 기상으로 에탄을 에틸렌 및 아세트산으로 촉매적으로 전환시키는 단계를 포함하는 방법을 제공하고, 여기서 촉매는 실험식 MoV a Nb b Te c Z d O n 를 갖는다. The present invention provides a method comprising the step of catalytically converting ethane to ethylene and acetic acid in the gas phase at a temperature of 450° C. or less in the presence of oxygen, wherein the catalyst comprises the empirical formula MoV a Nb b Te c Z d O n . Have

在不存在分子氧下由丙烷生产丙烯酸的方法

本发明涉及一种在不存在分子氧下由丙烷生产丙烯酸的方法。所述方法其特征在于包括：将不存在分子氧并含有丙烷、蒸气以及必要时的惰性气体的气体混合物通过一种催化剂，所述催化剂含有钼、钒、碲、氧和至少另外一种元素X，该元素X选自铌、钽、钨、钛、铝、锆、铬、锰、铁、钌、钴、铑、镍、钯、铂、锑、铋、硼、铟和铈，所述气体混合物还通过一种式(II)所示的助催化剂：Mo 1 Bi a ′Fe b ′Co c ′Ni d ′K e ′Sb f ′Ti g ′Si h ′Ca i ′Nb j ′Te k ′Pb I ′W m ′Cu n ′。本发明还涉及含有所述催化剂和助催化剂的固体催化剂组合物以及所述组合物在从丙烷制备丙烯酸中的应用。

Способ приготовления смешанных металлоксидных катализаторов окислительного аммонолиза и/или окисления низших алканов

1. Способ приготовления твердого предшественника смешанного оксидного катализатора получения акрилонитрила или метакрилонитрила из пропана или изобутана окислительным аммонолизом в газовой фазе, причем катализатор содержит элементы: молибден (Мо), ванадий (V), сурьму (Sb), ниобий (Nb), кислород (О), включающий приготовление реакционной смеси, содержащей соединение молибдена, соединение ванадия, соединение сурьмы и пероксид водорода, причем реакционную смесь готовят путем контактирования любого одного из соединений сурьмы, молибдена и ванадия с пероксидом водорода до смешения с исходными соединениями остальных элементов, содержащихся в смешанном оксидном катализаторе, и пероксид водорода берут в таком количестве, чтобы мольное соотношение пероксида водорода и сурьмы в катализаторе находилось в интервале 0.01-20; и сушку полученной смеси с образованием твердого предшественника. ! 2. Способ по п.1, в котором соединение молибдена приводят в контакт с пероксидом водорода с образованием реакционной смеси Мо-пероксид, а соединение ванадия смешивают с соединением сурьмы с образованием реакционной смеси V-Sb, и реакционную смесь V-Sb вводят в контакт с реакционной смесью Мо-пероксид с образованием объединенной реакционной смеси Mo-V-Sb. ! 3. Способ по п.2, в котором реакционную смесь V-Sb перед контактированием с реакционной смесью Мо-пероксид нагревают с обратным холодильником при температуре от примерно 80°С до примерно температуры кипения в течение примерно 15-45 мин. ! 4. Способ по п.2, в котором реакционную смесь V-Sb перед контактированием с реакционной смесью Мо-пероксид нагревают при температуре примерно 90°С в течение примерн� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2011 107 438 (13) A (51) МПК B01J 23/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (71) Заявитель(и): ИНЕОС ЮЭсЭй ЭлЭлСи (US) (21)(22) Заявка: 2011107438/04, 28.07.2009 Приоритет(ы): (30) Конвенционный приоритет: 01.08.2008 US 61/137,716 R U (54) СПОСОБ ...

Mixed oxide catalysts for catalytic oxidation in gas phase

FIELD: process engineering. SUBSTANCE: this invention relates to production of aldehydes and, at appropriate conditions, of acids. Proposed method comprises catalytic oxidation of alkanes or mixed thereof by air or oxygen, if necessary, in the presence of inert gases, steam or reaction offgas at higher temperatures using oxide catalyst. EFFECT: higher yield of, primarily, acrolein or mix of acrolein and acrylic acid. 4 cl, 11 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 480 280 (13) C2 (51) МПК B01J B01J B01J B01J B01J B01J B01J ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ B01J C07C (12) ОПИСАНИЕ 23/28 (2006.01) 23/887 (2006.01) 27/057 (2006.01) 23/26 (2006.01) 27/188 (2006.01) 23/24 (2006.01) 23/652 (2006.01) 37/03 (2006.01) 51/215 (2006.01) ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2009118819/04, 17.10.2007 (24) Дата начала отсчета срока действия патента: 17.10.2007 (73) Патентообладатель(и): ЭВОНИК ДЕГУССА ГМБХ (DE) (43) Дата публикации заявки: 20.02.2011 Бюл. № 5 2 4 8 0 2 8 0 (45) Опубликовано: 27.04.2013 Бюл. № 12 2 4 8 0 2 8 0 R U (85) Дата начала рассмотрения заявки PCT на национальной фазе: 20.05.2009 C 2 C 2 (56) Список документов, цитированных в отчете о поиске: US 3776952 A, 04.12.1973. FR 1447982 A, 05.08.1966. GB 1086523 F, 11.10.1967. GB 1286083 A, 16.08.1972. ЕР 1075871 А, 14.02.2001. WO 2007/042369 A, 19.04.2007. RU 2135280 C1, 27.08.1999. SU 1112618 A1, 30.09.1994. (86) Заявка PCT: EP 2007/061062 (17.10.2007) (87) Публикация заявки РСТ: WO 2008/046843 (24.04.2008) Адрес для переписки: 105082, Москва, Спартаковский пер., 2, стр. 1, секция 1, эт.3, "Евромаркпат" (54) СМЕШАННЫЕ ОКСИДНЫЕ КАТАЛИЗАТОРЫ ДЛЯ КАТАЛИТИЧЕСКОГО ОКИСЛЕНИЯ В ГАЗОВОЙ ФАЗЕ (57) Реферат: Настоящее изобретение относится к способу получения альдегидов и при определенных условиях кислот. Описан способ получения альдегидов и при определенных условиях кислот путем каталитического окисления алканов или смесей алканов воздухом либо кислородом при необходимости в присутствии инертных газов, ...

Pulsed oxidative dehydrogenation process

The present invention provides a continuous process for the oxidative dehydrogenation of a lower paraffin to a lower olefin, preferably alpha olefin by sequentially providing pulses of an oxygen containing gas, an inert gas, the paraffin, and inert gas in the presence of a catalyst that preferably has the ability to hold and release oxygen, so that the paraffin and the oxygen do not directly mix in the reactor.

烃的气相接触氧化催化剂、其制备方法以及使用该催化剂的烃的气相氧化方法

本发明提供了一种具有改进的产率和选择性的用于烃的气相接触氧化催化剂、其制备方法以及使用该催化剂的烃的气相氧化方法。该催化剂包含Mo、V、Te和Nb的复合金属氧化物；以及附着于所述复合金属氧化物上的钨或氧化钨，其中，附着于所述复合金属氧化物上的钨与在所述复合金属氧化物中包含的钼的原子摩尔比在0.00001∶1至0.02∶1的范围内。

钼-碲-钒-铌基odh催化剂的制备方法

可通过以下原位制备高活性ODH催化剂或前体而不分离中间体物种：在约3.3至7.5的pH下混合Mo、Te的溶液，将所得溶液的pH调回到约5，并添加VOSO 4 并添加Nb 2 O 5 和草酸的溶液，并在受控压力的水热法中处理所得的前体浆体以获得最终的催化剂，然后可将其从浆体中分离出来。