КАТАЛИЗАТОРЫ, КОТОРЫЕ СОДЕРЖАТ ГАЛОГЕНИДСОДЕРЖАЩИЕ ВОЛЬФРАМАТЫ ЩЕЛОЧНЫХ МЕТАЛЛОВ, ДЛЯ СИНТЕЗА АЛКИЛМЕРКАПТАНОВ И СПОСОБ ИХ ПРИГОТОВЛЕНИЯ

Изобретение относится к катализатору, содержащему вольфрамат щелочного металла, содержащему по меньшей мере один галогенид, где щелочнометаллический компонент выбран из группы, включающей Cs, Rb, или под щелочнометаллическим компонентом подразумевается комбинация из двух связанных щелочных металлов, в том числе и в отличном от 1:1 соотношении между ними, выбранная из группы, включающей а) калий и цезий, б) натрий и цезий, в) рубидий и цезий. Также изобретение раскрывает способ приготовления содержащего вольфрамат щелочного металла нанесенного катализатора и способ получения алкилмеркаптанов. Катализатор обладает высокой активностью и селективностью, что позволяет повысить выход алкилмеркаптанов и экономическую эффективность процесса их получения. 3 н. и 25 з.п. формулы, 1 табл.

СПОСОБ ФТОРИРОВАНИЯ НИЗШИХ АЛИФАТИЧЕСКИХ ФТОРУГЛЕВОДОРОДОВ

Использование: в качестве хладагента, распыляющего агента, реактивного топлива. Реагент 1 низший алифатический фторуглеводород. Реагент 2 фтористый водород. Условия синтеза: катализатор фторирования - частично фторированный оксид хрома, содержащий металлсодержащую добавку рутений или платину, 290 380°С. Катализатор обладает высокой производительностью и высоким сроком службы. 5 з.п. ф-лы.

СПОСОБ ГИДРОДЕХЛОРИРОВАНИЯ ДЛЯ ПОЛУЧЕНИЯ ДИГИДРОФТОРИРОВАННЫХ ОЛЕФИНОВ

... 1. Способ получения фторсодержащих олефинов, включающий контакт хлорфторалкена формулы RCCl=CClR, где каждый Rявляется перфторалкильной группой, независимо выбранной из группы, содержащей CF, CF, n-CF, i-CF, n-CF, i-CFи t-CF, с водородом в присутствии катализатора при температуре, достаточной, чтобы вызвать замещение заместителей хлора хлорфторалкена водородом, для получения фторсодержащего олефина формулы E- или Z-RCH=CHR, где каждый Rи Rявляются перфторалкильными группами, независимо выбранными из группы, содержащей CF, CF, n-CF, i-CF, n-CF, i-CFи t-CF, где указанный катализатор является композицией, включающей хром и никель.2. Способ по п.1, где указанный катализатор является композицией, включающей от приблизительно 10% до приблизительно 90% хрома и от приблизительно 90% до приблизительно 10% никеля.3. Способ по п.1, где каталитическая композиция дополнительно включает щелочной металл, выбранный из калия, цезия и рубидия.4. Способ по п.3, где указанный щелочной металл составляет от ...

VERFAHREN ZUR HERSTELLUNG VON 1,1,1,2,2-PENTAFLUOROETHAN

PRODUCTION OF A HYDRAULIC TREATMENT CATALYST.

CATALYST AND PROCEDURE FOR THE HYDROGEN TREATMENT.

PROCESS FOR THE MANUFACTURE OF 1,1,1,2-TETRAFLUOROETHANE

Process for preparing pentafluoroethane

PREPARATION OF DIESTERS OF (METH)ACRYLIC ACID FROM EPOXIDES

The application relates to a process for preparing a (meth)acrylic acid diester by reacting a (meth)acrylic acid anhydride with an epoxide in the presence of a catalyst system comprising a first and/or second catalyst in combination with a co-catalyst. The first catalyst is a halide of Mg or a trifluoromethanesulfonate of a rare earth element; the second catalyst is a Cr(lll) salt; and the co- catalyst is a tertiary amine, a quaternary ammonium salt, a tertiary phosphine or a quaternary phosphonium salt.

PROCESS FOR THE PREPARATION OF TETRAFLUORO-1,1,1,2-ETHANE

L'invention concerne la fabrication du tétrafluoro-1,1,1,2 éthane (134a) par fluoration catalytique du chloro-1-trifluoro-2,2,2-éthane (F133a) en phase gazeuse. On utilise un catalyseur mixte composé d'oxydes, halogénures et/ou oxyhalogénures de nickel et de chrome déposés sur un support constitué de fluorure d'aluminium ou d'un mélange de fluorure d'aluminium et d'alumine. Le catalyseur est préalablement activé par séchage et par fluoration au moyen d'acide fluorhydrique. Ce catalyseur mixte permet d'obtenir une excellente sélectivité en F134a avec une productivité élevée.

PROCESS FOR THE FLUORINATION OF PERCHLOROETHYLENE OR PENTACHLOROETHANE

L'invention concerne la fluoration catalytique du perchloréthylène ou du pentachloréthane en phase gazeuse au moyen d'acide fluorhydrique. On utilise un catalyseur mixte composé d'oxydes, d'halogénures et/ou d'oxyhalogénures de nickel et de chrome, déposés sur un support constitué de fluorure d'aluminium ou d'un mélange de fluorure d'aluminium et d'alumine, ledit catalyseur étant préalablement activé par séchage et par fluoration au moyen d'acide fluorhydrique.

Verfahren zur Herstellung von organischen Isocyanaten und Katalysator für die Ausführung des Verfahrens

Verfahren zur Herstellung aromatischer Isocyanate

ELECTROCHEMICAL HYDROXIDE SYSTEMS AND METHODS USING METAL OXIDATION

COMPOSITIONS OF OXYFLUORIDE OR CHROMIUM FLUORIDE CATALYSTS, PREPARATION AND USE THEREOF IN GAS PHASE PROCESSES

La présente invention concerne un procédé de modification de la distribution en fluor dans un composé hydrocarbure en présence d'un catalyseur, caractérisée par l'utilisation comme catalyseur d'une composition solide comprenant au moins un composant contenant de l'oxyfluorure ou du fluorure de chrome de formule CrxM(1-x)OrFs, où 2r+s est supérieur ou égal à 2,9 et inférieur à 6, M est un métal choisi dans les colonnes 2 à 12 du tableau périodique des éléments, x vaut de 0,9 à 1, s est supérieur à 0 et inférieur ou égal à 6 et r est supérieur ou égal à 0 et inférieur à 3, ladite composition solide ayant une cristallinité inférieure à 20 % en poids. La présente invention se rapporte aussi à la composition solide per se.

ESTERIFICATION PROCESS

히드로클로로플루오로카본의 촉매적 탈염화수소화

... 탈염화수소화 방법이 기재되어 있다. 상기 방법은 RfCHClCH2Cl을 반응 구역에서 크로뮴 옥시플루오라이드 촉매와 접촉시켜 RfCCl=CH2를 포함하는 생성물 혼합물을 생성하는 것을 포함하고, 여기서 Rf는 퍼플루오린화된 알킬 기이다.

METAL CATALYST COMPOSITION FOR PRODUCING FURFURAL DERIVATIVES FROM RAW MATERIALS OF LIGNOCELLULOSIC BIOMASS, AND METHOD FOR PRODUCING FURFURAL DERIVATIVES USING THE COMPOSITION

The present invention relates to a metal catalyst composition for producing furfural derivatives from raw materials of lignocellulosic biomass, and to a method for producing furfural derivatives using the composition. The metal catalyst composition comprises ruthenium chloride (RuCl3) and chromium chloride (CrCl2), wherein the chromium chloride (CrCl2) is 300 to 500 weight parts with respect to 100 weight parts of ruthenium chloride (RuCl3). According to the present invention, metal catalysts of multiple types are mixed at an optimum ratio, thus producing furfural derivatives from raw materials of lignocellulosic biomass through a simple reaction process performed in a single reaction device, which might otherwise require multistep processes such as pretreatment and simple saccharification processes as in conventional processes for producing furfural derivatives.

Cerous chloride-chromic oxide catalyst for producing chlorine, methods for producing the same and a method for producing chlorine

A novel cerous chloride-chromium oxide catalyst useful for oxidizing hydrogen chloride to chlorine. The catalyst is prepared by the reaction of chromium trioxide and cerous chloride with ethanol and calcining the reaction product. The catalyst is also prepared by the reaction of chromium trioxide with ethanol, then calcination and impregnation of the resultant chromic oxide with aqueous solution of cerous chloride. The obtained catalyst exhibits high activity at low reaction temperature.

PROCESSES FOR THE MANUFACTURE OF 1,1,1,3,3- PENTAFLUOROPROPENE, 2-CHLORO-PENTAFLUOROPROPENE AND COMPOSITIONS COMPRISING SATURATED DERIVATIVES THEREOF

A process is disclosed for producing the pentafluoropropenes of the formula CF 3 CX═CF 2 , where X is H or Cl. The process involves hydrodehalogenating CF 3 CCl 2 CF 3 with hydrogen at an elevated temperature in the vapor phase over a catalyst comprising an elemental metal, metal oxide, metal halide and/or metal oxyhalide (the metal being copper, nickel, chromium and the halogen of said halides and said oxyhalides being fluorine and/or chlorine). Processes for producing the hydrofluorocarbons CF 3 CH 2 CHF 2, CF 3 CHFCF 3 and CF 3 CH 2 CF 3 are also disclosed which involve (a) hydrodehalogenating CF 3 CCl 2 CF 3 with hydrogen as indicated above to produce a product comprising CF 3 CC1═CF 2, CF 2 CH═CF 2 , HCl and HF; and (b) either reacting the CF 3 CCl═CF 2 and/or CF 3 CH═CF 2 produced in (a) in the vapor phase with hydrogen to produce CF 3 CH 2 CHF 2 reacting the CF 3 CC 1═CF 2 produced in (a) with HF to produce CF 3 CHFCF 3, or reacting the CF 3 CH═CF 2 produced in (a) with HF to produce ...

Processes for the manufacture of 1,1,1,3,3-pentafluoropropene, 2-chloro-pentafluoropropene and compositions comprising saturated derivatives thereof

Disclosed are azeotropic compositions comprising CF3CHFCF3 and HF. Also disclosed are compositions and a process for producing compositions comprising (c1) CF3CHFCF3, CF3CH2CF3, or CHF2CH2CF3, and (c2) at least one saturated halogenated hydrocarbon and or ether having the formula: CnH2n+2-a-bClaFbOc wherein n is an integer from 1-4, a is an integer from 0-2n+1, b is an integer from 1-2n+2a, and c is 0 or 1, provided that when c is 1 then n is an integer from 2-4, and provided that component (c2) does not include the selected component (c1) compound, wherein the molar ratio of component (c2) to component (c1) is between about 1:99 and a molar ratio of HF to component (c1) in an azeotrope or azeotrope-like composition of component (c1) with HF. The process involves (A) combining (1) the azeotropic composition with (ii) the fluorination precursor to component (c2); and (B) reacting a sufficient amount of the HF from the azeotrope or azeotrope-like composition (1) with the precursor component ...

Mixed fluorination catalyst

Mixed fluorination catalyst comprising one or more nickel and chromium oxides, halides and/or oxyhalides deposited on a support composed of aluminium fluoride or of a mixture of aluminium fluoride and alumina, characterized in that the weight of nickel/weight of chromium ratio is between 0.08 and 0.25, preferably between 0.1 and 0.2.

Efficient catalytic greenhouse gas-free hydrogen and aldehyde formation from alcohols

Catalytic preparation of hydrogen and aldehyde(s) from alcohols, including bioalcohols, without production of carbon monoxide or carbon dioxide.

CATALYTIC PRODUCTION PROCESSES FOR MAKING 1,2,3,3,3-PENTAFLUOROPROPENE

КАТАЛИТИЧЕСКОЕ ГАЗОФАЗНОЕ ФТОРИРОВАНИЕ

Изобретение относится к способу фторирования, включающему чередующиеся реакционные стадии и стадии регенерации, в котором реакционные стадии включают взаимодействие хлорированного соединения с фтористым водородом в газовой фазе в присутствии катализатора фторирования с получением фторированного соединения, и стадии регенерации включают контакт катализатора фторирования с содержащим окислитель газовым потоком. Катализатор фторирования представляет собой оксифторид хрома, оксиды хрома, фториды хрома и их смеси, и дополнительно включает сокатализатор, выбранный из Co, Zn, Mn, Mg, Ni или их смесей, и в котором указанный сокатализатор предпочтительно присутствует в количестве, составляющем приблизительно от 1 до 10% массы указанного катализатора фторирования. Хлорированное соединение выбирают из 2-хлор-3,3,3-трифтор-1-пропена, 1,1,1,2,3-пентахлорпропана, 1,1,2,2,3-пентахлорпропана, 2,3-дихлор-1,1,1-трифторпропана, 2,3,3,3-тетрахлор-1-пропена и 1,1,2,3-тетрахлор-1-пропенам, и фторированное соединение ...

СПОСОБ ПРИГОТОВЛЕНИЯ СМЕШАННЫХ МЕТАЛЛОКСИДНЫХ КАТАЛИЗАТОРОВ ОКИСЛИТЕЛЬНОГО АММОНОЛИЗА И/ИЛИ ОКИСЛЕНИЯ НИЗШИХ АЛКАНОВ

Изобретение относится к способам приготовления предшественников катализаторов. Описаны способы приготовления твердых предшественников смешанных оксидных катализаторов получения акрилонитрила или метакрилонитрила из пропана или изобутана окислительным аммонолизом в газовой фазе, содержащих молибден (Мо), ванадий (V), сурьму (Sb), ниобий (Nb), кислород (О), включающие приготовление реакционной смеси, включающей указанные выше элементы, причем реакционную смесь готовят путем контактирования только одного из соединений сурьмы, молибдена и ванадия с пероксидом водорода до смешения с исходными соединениями остальных элементов, содержащихся в смешанных оксидных катализаторах, и пероксид водорода берут в таком количестве, чтобы мольное соотношение пероксида водорода и сурьмы в катализаторах находилось в интервале 0.01-20. Технический результат - увеличение активности и селективности катализаторов. 2 н. и 17 з.п. ф-лы, 1 ил., 4 табл., 12 пр.

КАТАЛИТИЧЕСКОЕ ГАЗОФАЗНОЕ ФТОРИРОВАНИЕ

КАТАЛИЗАТОР НА ОСНОВЕ ОКСИДА ЖЕЛЕЗА, ЕГО ПОЛУЧЕНИЕ И ПРИМЕНЕНИЕ В РЕАКЦИЯХ ДЕГИДРОГЕНИЗАЦИИ

... 1. Способ изготовления катализатора, включающий получение смеси, содержащей легированный регенерированный оксид железа и, по меньшей мере, один металл 1 группы или его соединение, где легированный регенерированный оксид железа получен путем добавления металла, не являющегося железом, или его соединения к смеси хлорида железа, и прокаливания аэрозоля этой смеси, где металл, не являющийся железом, выбран из группы, состоящей из церия и меди. ! 2. Способ по п.1, в котором смесь, содержащая хлорид железа, содержит от примерно 0,5 до примерно 100 миллимоль соединения металла, не являющегося железом, на моль железа. ! 3. Способ по любому из пп.1, 2, в котором соединение металла, не являющегося железом, включает хлорид меди. ! 4. Способ по любому из пп.1, 2, в котором соединение металла не являющегося железом, включает хлорид церия. ! 5. Способ по п.1, в котором металл 1 группы или его соединение включает калий. ! 6. Способ по п.1, дополнительно включающий добавление металла 2 группы или его соединения ...

КАТАЛИЗАТОР, ЕГО ПОЛУЧЕНИЕ И ПРИМЕНЕНИЕ

... 1. Способ получения катализатора, включающий приготовление смеси, содержащей оксид железа и, по меньшей мере, один металл 1 группы или его соединение, где оксид железа получен путем прокаливания аэрозоля смеси, содержащей галогенид железа и, по меньшей мере, 0,05 миллимоль металла 6 группы на моль железа. ! 2. Способ по п.1, в котором смесь содержит от примерно 0,5 до примерно 100 миллимоль металла 6 группы на моль железа. ! 3. Способ по любому из пп.1, 2, в котором металл 6 группы представляет собой молибден. ! 4. Способ по п.1, дополнительно включающий добавление металла 2 группы или его соединения в смесь оксида железа и металла 1 группы. ! 5. Способ по п.1, в котором галогенид железа включает кислый раствор хлорида железа. ! 6. Способ по п.1, в котором температура нагревания соответствует диапазону от примерно 300 до примерно 1000°С. ! 7. Способ по п.1, дополнительно включающий обжиг смеси при температуре от примерно 600 до примерно 1200°С. ! 8. Катализатор, полученный по способу по ...

Fluorierungsverfahren für halogenierte organische Verbindungen

HALOGENIDHALTIGE CAESIUMWOLFRAMATE CONTAINING CATALYSTS TO THE SYNTHESIS OF ALKYLMERCAPTAN AND PROCEDURES FOR YOUR PRODUCTION

PROCEDURE FOR THE PRODUCTION OF FLUOROETHAN

Process for preparing pentafluoroethane

Electrochemical hydroxide systems and methods using metal oxidation

There are provided methods and systems for an electrochemical cell including an anode and a cathode where the anode is contacted with a metal ion that converts the metal ion from a lower oxidation state to a higher oxidation state. The metal ion in the higher oxidation state is reacted with hydrogen gas, an unsaturated hydrocarbon, and/or a saturated hydrocarbon to form products.

ACTIVATION AND REGENERATION OF FLUORINATION CATALYSTS

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

A HYDROFINING CATALYST OF A DISTILLATE OIL AND PRODUCTION METHOD

The present invention discloses a hydrofining catalyst. The catalyst has the following composition based on the total weight of the entire catalyst composition: 1-5 % (wt.) nickel oxid e, 12-35 % (wt.) tungsten oxide, 1-9 % (wt.) fluorine, and the balancing amount of composite alumina. Said composit e alumina is composed of one or several kinds of micropore alumina and one or several kinds of macropore alumina, wherein the weight ratio of micropore alumina to macropore alumina is 75:25 to 50:50. The term "micropor e alumina" in the context means the alumina in which the volume of the pore of diameter less than 80 angstro m occupies more than 95 % of its total pore volume, while the term "macropore alumina" in the context means the alumina in which the volume of the pore of diameter 60-600 angstrom occupies more that 70 % of its total pore volume. The pore distribution mentioned above is determined by BET method of nitrogen adsorption at low temperature. This catalyst is especially suitable ...

ELECTROCHEMICAL DEVICES AND METHODS BASED ON HYDRO KSIDOV WITH USE OF METAL OXIDATION

GAS-PHASE CATALYTIC FLUORINATION WITH CHROMIUM CATALYSTS

SCR Catalyst for diesel vehicle tail gas denitration and preparation method thereof

Processes for purifying chlorofluorinated compounds and processes for purifying CF3CFHCF3

PROCESS FOR PRODUCING 2, 3, 3, 3 A-TETRAFLUOROPROPENE.

MANUFACTORING PROCESS OF the 1,1-DIFLUOROETHANE

Fluorination process of perchlorethylene or [...]

L'invention concerne la fluoration catalytique du perchloréthylène ou du pentachloréthane en phase gazeuse au moyen d'acide fluorhydrique. On utilise un catalyseur mixte composé d'oxydes, halogénures et/ou oxyhalogénures de nickel et de chrome déposés sur un support constitué de fluorure d'aluminium ou d'un mélange de fluorure d'aluminium et d'alumine.

CATALYST Of HYDRORAFFINAGE AND/OR HYDROCONVERSION INCLUDING/UNDERSTANDING UNENOUVELLE PHASE ACTIVATES IN THE FORM OF SOLID SOLUTION SULPHURIZES

La présente invention concerne un catalyseur d'hydroraffinage et/ou hydroconversion de charges hydrocarbonées dont la phase active comprend au moins une solution solide sulfure de molybdène et de tungstène au sein du même feuillet, de formule générale approchée MoxW1-xSy, où x est un nombre strictement compris entre 0 et 1 et y est un nombre compris entre 1,4 et 2,6 et de préférence au moins un élément du groupe VIII.

CATALYST PREPARED BY GRINDING REAGENT

PRODUCING METHOD OF HALOGENATED PROPANE CONTAINING FLUORINE SUBSTITUTED AT TERMINAL CARBON

PURPOSE: A supplying method of CCl4CH2CCl3(HCC-230fa), liquid with high boiling point, to catalyst bed directly, is known. But the method causes substantially degradation of HCl, CCl3CH=CCl2 and especially material with high boiling point(for example, chlorinated 6-carbon compound and tar). Also the production of HFC-236fa in catalytic reactor by substituting chlorine in HCC-230fa with fluorine, may cause heat management problem. CONSTITUTION: The producing method of Formula CF3CHXCF(3-z)Yz (wherein X and Y are selected independently from a group consisting of H and Cl, z is 0 or 1) comprises the steps of: 1) starting material selected from a group consisting of Formula CF3CHXCF(3-z)Yz and its mixture contact with hydrogen fluoride to produce fluorinated product of the starting material, 2) saturated compound produced by the process and compound selected from a group consisting of olefin compounds contact with hydrogen fluoride of vapor phase at 200 to 400°C in the presence of fluorinating ...

Method for preparing metal fluoride catalysts and dehydrofluorination method using the same

Disclosed is a method for preparing a metal fluoride catalyst as a dehydrofluorination catalyst having high activity under a mild condition using a trifluoroacetic acid solution with no use of HF gas having fluidity and corrosive property. Disclosed also is a dehydrofluorination method for preparing HFO-1225ye from HFP-236ea by using the catalyst with high efficiency.

СПОСОБЫ КАТАЛИТИЧЕСКОГО ПОЛУЧЕНИЯ ГЕКСАФТОРПРОПЕНОВ

Настоящее изобретение относится к способу получения гидрофторпропена, включающему: (а) приведение в контакт гексафторпропана, представляющего собой 1,1,1,2,2,3-гексафторпропан, с хромовым оксифторидным катализатором в реакторе с получением смеси продуктов, содержащей 1,2,3,3,3-пентафторпропен, указанная смесь включает Z-HFC-1225ye и Е-HFC-1225ye, и (b) извлечение упомянутого 1,2,3,3,3-пентафторпропена из упомянутой смеси продуктов, где упомянутый катализатор содержит щелочной металл в количестве приблизительно 2000 ч./млн или менее. Также изобретение относится к способу получения гидрофторпропена, включающему: (а) приведение в контакт 1,1,1,2,2-пентафторпропана с хромовым оксифторидным катализатором в реакторе с получением смеси продуктов, включающей 2,3,3,3-тетрафторпропен; и (b) извлечение упомянутого 2,3,3,3-тетрафторпропена из упомянутой смеси продуктов, где упомянутый катализатор содержит щелочной металл в количестве приблизительно 2000 ч./млн или менее. Техническим результатом настоящего ...

СПОСОБ ПОЛУЧЕНИЯ ПЕНТАФТОРЭТАНА

FIELD: organic chemistry, chemical technology. SUBSTANCE: invention relates to method of synthesis of pentafluoroethane containing 1-chloropentafluoroethane in the amount below 0.02 wt. %. Pentafluoroethane is synthesized in the process of conversion of tetrafluorochloroethane CF 3 CHC1F in gaseous phase in the presence of chrome oxide catalyst (Cr 2 O 3 ) applied on carrier containing AlF 3 followed by its isolation from compounds obtained. The above mentioned carrier has fluorine content corresponding to at least to 90% of AlF 3 with respect to total carrier weight. Process is carried out at 140-300 C and time contact for 0.1-30 s. Synthesized pentafluoroethane has small amount of 1-chloropentafluoroethane. EFFECT: improved method of synthesis, small amount of impurity. 7 cl, 5 ex эгеч9гс ПпПы с» (19) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ ВИ `” 2 165 916 (51) МПК” (13) С2 С 07С 17/25, 19/08 (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 96122564/04, 27.11.1996 (24) Дата начала действия патента: 27.11.1996 (30) Приоритет: 28.11.1995 1Т М1 95 А 002484 (43) Дата публикации заявки: 27.01.1999 (46) Дата публикации: 27.04.2001 (56) Ссылки: ЕР 0612709 АЛ, 31.08.94. КУ 95113273 АЛ, 20.11.96. ЕР 0508631 АЛ, 14.10.92. (98) Адрес для переписки: 121087, Москва, а/я 33, Курышеву В.В. (71) Заявитель: Аусимонт С.п.А. (1Т) (72) Изобретатель: КУЦЦАТО Паоло (1!Т) (73) Патентообладатель: Аусимонт С.п.А. (1Т) (74) Патентный поверенный: Курышев Владимир Васильевич (54) СПОСОБ ПОЛУЧЕНИЯ ПЕНТАФТОРЭТАНА (57) Изобретение относится к способу получения пентафторэтана, содержащего 1-хлор-пентафторэтана меньше 0,02% по весу. Пентафторэтан получают процессом превращения тетрафторхлорэтана СЕ 3СНЕЕ в газовой фазе в присутствии хромового окисного катализатора (Сг2Оз), нанесенного на носитель, включающий АР, с последующим выделением его из полученных продуктов. Причем упомянутый носитель имеет содержание фтора, соответствующее по крайней мере 90% Аз по ...

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 ...

СПОСОБЫ ПРОИЗВОДСТВА 1,1,1,2,3-ПЕНТАФТОРПРОПИЛЕНА И СПОСОБЫ ПРОИЗВОДСТВА 1,1,1,2,3-ПЕНТАФТОРПРОПАНА

Настоящее изобретение обеспечивает способы производства 1,1,1,2,3-пентафторпропилена, отличающиеся тем, что реакция удаления HF происходит при взаимодействии 1,1,1,2,3,3-гексафторпропана в газообразном состоянии с активным углем или с активным углем с добавкой соли металла. 1,1,1,2,3-пентафторпропилен согласно данному изобретению можно получить из доступного 1,1,1,2,3,3-гексафторпропана эффективными в смысле затрат промышленными способами с высокими выходами. Настоящее изобретение обеспечивает также способы производства 1,1,1,2,3-пентафторпропана, отличающиеся тем, что включают восстановление 1,1,1,2,3-пентафторпропилена водородом в присутствии катализатора гидрирования, состоящего из палладия с добавкой одного или более металлов, выбранных из серебра, меди, золота, теллура, цинка, хрома, молибдена и таллия, или в присутствии родиевого катализатора. Требуемый продукт согласно этим изобретениям можно получить при высокой реактивности и высокой селективности.

КАТАЛИЗАТОР ОКИСЛИТЕЛЬНОГО ДЕГИДРИРОВАНИЯ ЭТАНА В ЭТИЛЕН И СПОСОБ ЕГО ПОЛУЧЕНИЯ

Изобретение относится к получению этилена из этана путем каталитической окислительной конверсии с раздельной подачей сырья и окислителя и одновременного получения технического азота из воздуха и может использоваться в химической и нефтехимической отраслях промышленности. Предложен катализатор окислительного дегидрирования этана в этилен, содержащий оксиды ванадия и молибдена, нанесенный на оксид алюминия, который дополнительно модифицирован фтором при соотношении F/Al, равном 1/1000-1/10, при следующем соотношении компонентов, % мас.: оксиды ванадия и молибдена 5-40, модифицированный фтором оксид алюминия - остальное, при массовом отношении молибдена к ванадию, равном 3-6. Катализатор дополнительно может содержать оксид ниобия в количестве 0,1-5 % мас. Для получения катализатора оксид алюминия предварительно обрабатывают раствором фторида аммония с получением модифицированного фтором оксида алюминия. Затем растворяют в воде парамолибдат аммония и метаванадат аммония, добавляют модифицированный ...

КАТАЛИТИЧЕСКОЕ ГАЗОФАЗНОЕ ФТОРИРОВАНИЕ

... 1. Способ фторирования, включающий чередующиеся реакционные стадии и стадии регенерации, в котором реакционные стадии включают взаимодействие хлорированного соединения с фтористым водородом в газовой фазе в присутствии катализатора фторирования с получением фторированного соединения, и стадии регенерации включают приведение в контакт катализатора фторирования с содержащим окислитель газовым потоком.2. Способ фторирования по п.1, включающий предварительную стадию активации, которая включает приведение в контакт катализатора фторирования с содержащим окислитель газовым потоком.3. Способ по п.1 или 2, в котором содержащий окислитель газовый поток стадии активации и/или стадий регенерации представляет собой кислородсодержащий газовый поток.4. Способ по п.1 или 2, в котором стадия активации и/или стадии регенерации включают приведение в контакт катализатора фторирования с содержащим окислитель газовым потоком по меньшей мере в течение 2 часов, предпочтительно по меньшей мере в течение 4 часов ...

Verfahren zur Herstellung von Isocyanatverbindungen

Verfahren zur Herstellung von Halogenaromaten

PROCEDURE FOR THE PRODUCTION OF 1,1,1,2 - TETRAFLUORETHAN.

BINUCLEAR METATHESIS CATALYSTS

CATALYST AND PROCESSES FOR OLEFIN TRIMERIZATION

A process is provided to modify an olefin production catalyst system which comprises contacting an olefin production catalyst system with ethylene prior to use. A second embodiment of the invention comprises contacting an aluminium alkyl and a pyrrole-containing compound prior to contacting a chromium containing compound and prior to contacting an olefin. A process also is provided to trimerize and/or oligomerize olefins with the novel, modified olefin catalyst production systems. These modified olefin production catalyst systems can produce less solids, such as, for example, polymer, during a trimerization reaction.

IRON OXIDE CATALYST, ITS PREPARATION AND USE IN DEHYDROGENATION REACTIONS

A process for preparing a catalyst which process comprises preparing a mi xture comprising iron oxide and at least one Column 1 metal or compound ther eof, wherein the iron oxide is obtained by heating a mixture comprising an i ron halide and at least 0.05 millimole of a metal chloride that is converted to a metal oxide under the heating conditions per mole of iron; a catalyst made by the above described process; a process for the dehydrogenation of an alkylaromatic compound which process comprises contacting the alkylaromatic compound with the catalyst; and a method of using an alkenylaromatic compou nd for making polymers or copolymers, in which the alkenylaromatic compound has been produced by the dehydrogenation process.

FLUORINATION CATALYST AND FLUORINATION PROCESS

A fluorination catalyst comprising indium, chromium, oxygen and fluorine as essential constituent elements thereof. The catalyst is prepared by fluorinating a catalyst precursor comprising indium and chromium elements by bringing it into contact with hydrogen fluoride or a fluorine-containing halogenated hydrocarbon at a temperature of 300 to 500.degree.C. A halogenated hydrocarbon is fluorinated by bringing it into contact with hydrogen fluoride in a gaseous phase in the presence of the catalyst.

HIGH POROSITY, HIGH SURFACE AREA ISOMERIZATION CATALYST AND ITS USE

A novel, high porosity, high surface area catalyst is disclosed which is useful in wax isomerization processes, especially for the production of high viscosity index, low pour point lubricating oil base stoc ks or blending stocks. The catalyst contains a catalytically active metal component selected from the group consisting of Group VIB and Group VIII metals, and mixtures thereof, preferably Group VIII metals, and mixtures thereof, more preferably noble Group VIII metals and mixtures thereof, most preferably platinum, which catalytically active metal component is present in th e range of about 0.01 to 5.0 wt.%, and a fluorine content in the range of about 0.01 to about 10.0. The catalyst employs a refractory meta l oxide support material, one preferably predominantly (i.e., at least 50 wt.%) alumina, most preferably completely alumi na, e.g., gamma or eta alumina. The finished catalyst has a porosity, expressed in terms of pore volume, of at least about 0.50 cc/gram an d a surface area ...

CHROMIUM-BASED FLUORINATION CATALYST, PROCESS FOR PRODUCING THE CATALYST, AND FLUORINATION PROCESS USING THE CATALYST

CHROMIUM-BASED FLUORINATION CATALYST. PROCESS FOR PRODUCING THE CATALYST, AND FLUORINATION PROCESS USING THE CATALYST A halogenated hydrocarbon having 1 to 4 carbon atoms is brought into contact with hydrogen fluoride in a gaseous phase in the presence of a catalyst prepared by firing a substance composed mainly of chromium(III) hydroxide in the presence of hydrogen at a temperature of 350 to 500.degree.C or a catalyst prepared by heat-treating the above substance in an inert gas stream at a temperature of 100 to 600.degree.C and then firing the heat-treated compound in the presence of hydrogen at the above temperature or any one of catalysts prepared by partially fluorinating the above catalysts.

PROCESS FOR FLUORINATING HALOGENATED HYDROCARBON

A halogenated hydrocarbon is effectively fluorinated by reacting the halogenated hydrocarbon with hydrogen fluoride in the presence of a fluorination catalyst which comprises a partially fluorinated chromium oxide containing at least one metal selected from the group consisting of ruthenium and platinum.

PROCESS FOR FLUORINATING HALOGENATED HYDROCARBON

The present invention is directed to a halogenated hydrocarbon which is effectively fluorinated by reacting the halogenated hydrocarbon with hydrogen fluoride in the presence of a fluorination catalyst. The catalyst comprises a partially fluorinated chromium oxide containing at least one metal selected from the group consisting of ruthenium and platinum.

DISTILLATE HYDROCRACKING CATALYST AND PROCESS FOR THE PREPARATION OF THE SAME

The present invention relates to a hydrocracking catalyst containing nickel, tungsten, fluorine, zeolite as well as alumina. Said catalyst is composed of, based on the total weight of the catalyst, 0.5-5.0 wt.% fluorine, 2.5-6.0 wt.% nickel oxide, 10-38 wt.% tungsten oxide, and a catalyst carrier. Said carrier is composed of 20-90 wt.% alumina and 10-80 wt.% zeolite wherein the zeolite is mesopore or macropore zeolite of an acidity strength value 1.0-2.0 mmol/g determined by NH3-TPD, the alumina is the alumina of an acidi ty strength value 0.5-0.8 mmol/g determined by NH3-TPD. Said catalyst possesses good desulfurization activity , denitrogenation activity, and higher selectivity with respect to middle distillates than that of the prior art.

Using metal oxide electrochemical hydroxide system and method

Process of addition of the hydrocyanic acid to olefins and products obtained by this process

Catalyst stabilization of fluoridation

CATALYTIC GAS PHASE FLUORINATION WITH CATALYSTS BASED ON CHROMIUM

La présente invention concerne un procédé de fluoration d'un composé chloré comprenant les étapes de (a) mise en contact, dans un réacteur, dudit composé chloré avec du fluorure d'hydrogène en phase gazeuse en présence d'un catalyseur de fluoration pour produire un composé fluoré, et (b) régénération du catalyseur de fluoration utilisé à l'étape a), l'étape de régénération du catalyseur de fluoration comprenant (c) le traitement dudit catalyseur de fluoration avec un oxydant pour former un catalyseur de fluoration oxydé, et (d) le traitement du catalyseur de fluoration oxydé obtenu à l'étape (c) avec un mélange gazeux comprenant un agent réducteur.

HIGH PRESSURE CATALYST ACTIVATION METHOD AND CATALYST PRODUCED THEREBY

A process for the activation of a fluorination catalyst in which a catalyst precursor compound, supported or unsupported is first dried and thereafter activated by exposure to an activating agent at a pressure greater that about 100 psig and a temperature grater than about 100°C. The process is particularly suited to the activation of chromium (111) compounds, such as Cr2O3. The resulted dry, high-pressure activated catalyst was found to provide increase fluorination conversion, with higher selectivity of the desired product. © KIPO & WIPO 2009 ...

METHOD OF MAKING MIXED METAL OXIDE CATALYSTS FOR AMMOXIDATION AND/OR OXIDATION OF LOWER ALKANE HYDROCARBONS

PROCESSES FOR THE PREPARATION OF SILICON CONTAINING INTERMETALLIC COMPOUNDS AND INTERMETALLIC COMPOUNDS PREPARED THEREBY

Intermetallic compounds, such as metal silicides, e.g., PdSi and/or Pd2Si, can be selectively prepared in a two step process including the steps of (1 ) vacuum impregnating silicon with a metal halide, and (2) ball milling the product of step (1).

CATALYTIC PRODUCTION PROCESSES FOR MAKING TETRAFLUOROPROPENES AND PENTAFLUOROPROPENES

A process is disclosed for making CF3CF=CHF. The process involves contacting at least one hexafluoropropane selected from the group consisting of CF3CF2CH2F and CF3CHFCHF2 with a chromium oxyfluoride catalyst in a reactor to obtain a product mixture comprising CF3CF=CHF, and recovering CF3CF=CHF from the product mixture. A process is disclosed for making CF3CH=CHF. The process involves contacting CF3CH2CHF2 with a chromium oxyfluoride catalyst in a reactor to obtain a product mixture comprising CF3CH=CHF, and recovering CF3CH=CHF from the product mixture. A process is disclosed for making CF3CF=CH2. The process involves contacting CF3CF2CH3 with a chromium oxyfluoride catalyst in a reactor to obtain a product mixture comprising CF3CF=CH2, and recovering CF3CF=CH2 from the product mixture.

Hydrogen storage matter and manufacturing method and apparatus for the same

A hydrogen storage matter contains at least a nano-structured and organized lithium imide compound precursor complex. In the hydrogen stroge matter, the lithium imide compound precursor complex has been nano-structured and organized by mixing fine powder lithium amide with fine powder lithium hydride at a predetermined ratio to prepare a mixture as a starting material, and then processing the mixture by a predetermined complex formation processing method.

Method for Producing 1,2-Dichloro-3,3,3-Trifluoropropene

A method for producing 1,2-dichloro-3,3,3-trifluoropropene according to the present invention includes the step of reacting 1,1,2,3,3-pentachloropropene with a fluorinating agent where hydrogen fluoride is used as the fluorinating agent.

PROCESS FOR PREPARING FLUORINATION CATALYST

A process for preparing a fluorination catalyst using a low pressure activating step followed by a high pressure activating step.

КАТАЛИТИЧЕСКОЕ ГАЗОФАЗНОЕ ФТОРИРОВАНИЕ

Изобретение относится к способу фторирования для получения фторолефина, включающему предварительную стадию активации, которая включает приведение в контакт катализатора фторирования с содержащим окислитель газовым потоком, который не содержит фтористый водород, и чередующиеся реакционные стадии и стадии регенерации, в котором реакционные стадии включают взаимодействие хлорированного соединения с фтористым водородом в газовой фазе в присутствии катализатора фторирования с получением фторированного соединения, и стадии регенерации включают контакт катализатора фторирования с содержащим окислитель газовым потоком. Технический результат - повышение селективности процесса за счет регенерации катализатора в присутствии окислителя кислорода. 18 з.п. ф-лы, 2 табл., 7 пр.

Patent RU2019106451A3

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 37/02 B01J 37/08 B01J 27/02 B01J 21/00 C10G 45/00 (11) (13) 2019 106 451 A (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2019106451, 24.04.2017 (71) Заявитель(и): ЧАЙНА ПЕТРОЛЕУМ ЭНД КЕМИКАЛ КОРПОРЕЙШЕН (CN), РИСЕРЧ ИНСТИТУТ ОФ ПЕТРОЛЕУМ ПРОЦЕССИНГ, СИНОПЕК (CN) Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 12.10.2020 Бюл. № 29 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 12.04.2019 CN 2017/000318 (24.04.2017) (87) Публикация заявки PCT: A WO 2018/045693 (15.03.2018) Адрес для переписки: 119019, Москва, Гоголевский бульвар,11, Гизатуллина Евгения Михайловна R U (57) Формула изобретения 1. Способ получения катализатора гидрирования, предусматривающий стадии, на которых: (1) вводят в контакт первый активный металлический компонент, первый органический комплексообразующий агент и необязательный соагент с носителем и получают композиционный носитель; (2) прокаливают композиционный носитель и получают прокаленный композиционный носитель, в котором полное содержание углерода в расчете на сухой прокаленный композиционный носитель составляет 1 мас.% или менее, 0,5 мас.% или менее, 0,4 мас.% или менее, 0,3 мас.% или менее, 0,1 мас.% или менее, 0,08 мас.% или менее, 0,06 мас.% или менее, 0,04 мас.% или менее, 0,03 мас.% или менее, 0,01 мас.% или менее, или 0,005 мас.% или менее по отношению к сухой массе прокаленного композиционного носителя; и (3) вводят в контакт второй органический комплексообразующий агент с прокаленным композиционным носителем и получают катализатор гидрирования, и необязательно способ дополнительно предусматривает одну или несколько из стадий, на которых: (0) получают носитель; и (4) сульфурируют катализатор гидрирования. Стр.: 1 A 2 0 1 9 1 0 6 4 5 1 (54) КАТАЛИЗАТОР ГИДРИРОВАНИЯ, ЕГО ПОЛУЧЕНИЕ И ПРИМЕНЕНИЕ 2 0 1 9 1 0 6 4 5 1 (86) Заявка PCT: (72) Автор(ы): ЧЖАН, ...

Способ получения акриловой кислоты

FIELD: chemistry; electrical engineering. SUBSTANCE: invention relates to a one-step process for gas-phase oxidation of propane to form acrylic acid in the presence of a mixed metal oxide catalyst in excess of air oxygen relative to propane. Invention also relates to electrical engineering and can be used to electrically conduct current catalysts for gas-phase oxidation of propane and other catalytic processes with their use. Proposed method for producing acrylic acid in a flow reactor at atmospheric pressure and elevated temperature in the presence of a mixed metal oxide catalyst using a mixture of propane, air and water vapor as a gas feedstock, where a layer of a granular conductive composition catalyst Mo 1.0 V 0.37 Te 0.17 Nb 0.12 O 3 with a particle size of 0.4–0.8 mm is heated with a preheated gas feedstock with a volume ratio of propane to air of 1:10 and a partial pressure of water in a mixture of 170 Torr, while an alternating electric current is applied to the catalyst layer with a frequency in the range of 50–700 Hz, and the process is carried out at a temperature of 350–380 °C and a gas feedstock flow rate of 60 cm 3 /min. Method comprises using a quartz tubular flow reactor which has two adjacent zones-the preheating zone of the feedstock, the quartz head covered with a quartz nozzle and heated by an electric furnace, and a sequentially located reaction zone along which the current flow is fed to the catalytic layer. EFFECT: invention can be used to electrically conduct current catalysts for gas-phase oxidation of propane and other catalytic processes with their use. 1 cl, 1 dwg, 2 tbl, 9 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 644 158 C1 (51) МПК C07C 57/04 (2006.01) C07C 51/215 (2006.01) C07C 27/14 (2006.01) B01J 27/057 (2006.01) B01J 27/132 (2006.01) B01J 23/20 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C07C 51/215 (2006.01); C07C 27/14 (2006.01); B01J 27/057 (2006.01); B01J 27/132 ...

СПОСОБ ПОЛУЧЕНИЯ АКРОЛЕИНА ИЗ ГЛИЦЕРОЛА

... 1. Способ получения акролеина из глицерина, где дегидрирование глицерина проводят в присутствии катализатора MWOA, где MWO представляет собой смесь простых оксидов и/или смешанных оксидов вольфрама и по меньшей мере одного металла М, выбранного из циркония, кремния, титана, алюминия и иттрия, и А представляет собой одно или несколько оснований Льюиса, причем упомянутое основание Льюиса имеет формулу B(R)p(R)q(R)r, где В представляет собой элемент, выбранный из С, S, Ρ, О, N и галидов, R, Rи Rнезависимо друг от друга представляют собой Н, C-С-алкильную группу, О, ОН или OR, где R представляет собой C-С-алкильную группу и сумма р, q и r составляет от 0 до 4.2. Способ по п. 1, где M представляет собой по меньшей мере два или три металла, выбранных из циркония, кремния, титана, алюминия и иттрия.3. Способ по п. 1, где А выбрано из ионов фосфата HPO , x составляет от 0 до 2, НРО, ионов бората, F, Cl, Br, I, NH, CN, ионов сульфата, ионов карбоната, ионов карбоксилата, спиртов, алкоголят-ионов ...

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА ФТОРИРОВАНИЯ

... 1. Способ получения катализатора, пригодного для фторирования органического соединения, включающий обработку каталитически активного соединения первым активирующим агентом при примерно рабочей температуре и рабочем давлении катализатора при условиях, эффективных для достижения практически устойчивого состояния при указанных примерно рабочих температуре и давлении. 2. Способ по п.1, отличающийся тем, что указанный активирующий агент практически не содержит реакционно-способных органических соединений. 3. Способ по п.1, отличающийся тем, что указанная стадия обработки включает обработку соединения первым активирующим агентом при первом давлении, которое значительно ниже рабочего давления реакции фторирования органического соединения, и удаление из указанного каталитически активного соединения указанного первого активирующего агента. 4. Способ по п.1, отличающийся тем, что указанная стадия обработки дополнительно включает, после указанной стадии обработки при низком давлении, обработку указанного ...

VERFAHREN ZUR HERSTELLUNG VON 1,1,1,3,3-PENTAFLUORPROPAN

PREPARATION OF ORGANIC ISOCYANATES

... 1,245,480. Isocyanates. OLIN CORP. 13 Nov., 1968 [18 Dec., 1967], No. 53878/68. Heading C2C. Organic isocyanates are made by reacting an organic nitro compound with carbon monoxide at a raised temperature and pressure in the presence of a catalyst comprising a mixture of (a) a heteroaromatic compound containing 5 or 6 members in a ring containing carbon and 1 or 2 nitrogen atoms only and at least 2 double bonds, or a substitution product (including a fused-ring substitution product) or a salt of such a compound and (b) a halide or oxide of a platinum-group metal, silver or gold, or a complex of components (a) and (b). Additionally, the catalyst may comprise an oxide or oxides of vanadium, molybdenum, tungsten, niobium, chromium and tantalum.

PROCEDURE FOR ACTIVATING HALOGENIERTEN CATALYSTS, IN THE PROCEDURE MANUFACTURED CATALYSTS AND APPLICATION OF THESE CATALYSTS IN HYDROCARBON CONVERSIONS.

PROCEDURE FOR THE PRODUCTION OF PENTAFLUORETHAN

PRODUCTION OF A CARRIER FOR HYDRAULIC TREATMENT CATALYST

PROCEDURE FOR THE PRODUCTION OF 1,1,1,2,2 - PENTAFLUOROETHAN

Procedure for the production of organic isocyanates

Procedure for the production of organic isocyanates

Preparation of diesters of (meth)acrylic acid from epoxides

The application relates to a process for preparing a (meth)acrylic acid diester by reacting a (meth)acrylic acid anhydride with an epoxide in the presence of a catalyst system comprising a first and/or second catalyst in combination with a co-catalyst. The first catalyst is a halide of Mg or a trifluoromethanesulfonate of a rare earth element; the second catalyst is a Cr(lll) salt; and the co- catalyst is a tertiary amine, a quaternary ammonium salt, a tertiary phosphine or a quaternary phosphonium salt.

Process for the manufacture of 1,1,1,2-tetrafluoroethane

TITANIUM OXIDE PHOTOCATALYST, PROCESS FOR PRODUCING THE SAME AND APPLICATION

Electrochemical hydroxide systems and methods using metal oxidation

There are provided methods and systems for an electrochemical cell including an anode and a cathode where the anode is contacted with a metal ion that converts the metal ion from a lower oxidation state to a higher oxidation state. The metal ion in the higher oxidation state is reacted with hydrogen gas, an unsaturated hydrocarbon, and/or a saturated hydrocarbon to form products.

Process for fluorination of perchloroethylene or of pentachloroethane

HYDROTREATING CATALYST AND PROCESS

A hydrotreating catalyst is described which comprises at least one Group VI metal, metal oxide, or metal sulfide, and at least one Group VIII metal, metal oxide, or metal sulfide, supported on a carrier wherein (A) the catalyst comprises from about 10% to about 35% by weight of combined metal, and the atomic ratio of the Group VIII metal to Group VI metal is in the range of from about 0.5:1 to about 2:1; (B) the carrier comprises from about 0.5 to about 10 weight percent of halogen, from about 0.5 to about 5% by weight of silica and from about 85 to about 99% of alumina; and (C) the catalyst is characterized as having a median pore radius of from about 30 to about 65 Angstroms, and a surface area of from about 120 to about 180 m2/g. Also described are novel and improved procedures for preparing the carrier or support used to prepare the catalysts. The catalyst is useful in the production of lubricating oils from crude hydrocarbon oil stocks in that the hydrotreating process results in the ...

PROCESS FOR PRODUCING CHLOROTRIFLUOROETHYLENE

The present invention relates, at least in part, to a process for making chlorotrifluoroethylene (CFO-1113) from 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a). In certain aspects, the process includes dehydrochlorinating 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a) in the presence of a catalyst selected from the group consisting of (i) one or more metal halides; (ii) one or more halogenated metal oxides; (iii) one or more zero-valent metals or metal alloys; (iv) combinations thereof.

ELECTROCHEMICAL HYDROXIDE SYSTEMS AND METHODS USING METAL OXIDATION

There are provided methods and systems for an electrochemical cell including an anode and a cathode where the anode is contacted with a metal ion that converts the metal ion from a lower oxidation state to a higher oxidation state. The metal ion in the higher oxidation state is reacted with hydrogen gas, an unsaturated hydrocarbon, and/or a saturated hydrocarbon to form products.

Dehydrofluorination of pentafluoroalkanes to form tetrafluoroolefins

A method for producing a tetrafluoroolefin, such as 2,3,3,3-tetrafluoropropene (HFO-123434), comprises dehydrofluorinating a pentafluoroalkane in a gas phase in the presence of a catalyst comprising chromium oxyfluoride. In a preferred embodiment, 2,3,3,3-tetrafluoropropene (HFO-1234yf) is produced by forming a catalyst comprising chromium oxyfluoride by calcining CrF3?xH2O, where x is 1-10, in the presence of a flowing gas comprising nitrogen to form a calcined chromium oxyfluoride, and dehydrofluorinating 1,1,1,2,2-pentafluoropropane (HFC-245cb) in a gas phase in the presence of the catalyst to form the 2,3,3,3-tetrafluoropropene (HFO-1234yf).

PROCESS FOR PRODUCING CHLOROTRIFLUOROETHYLENE

The present invention relates, at least in part, to a process for making chlorotrifluoroethylene (CFO-1113) from 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a). In certain aspects, the process includes dehydrochlorinating 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a) in the presence of a catalyst selected from the group consisting of (i) one or more metal halides; (ii) one or more halogenated metal oxides; (iii) one or more zero-valent metals or metal alloys; (iv) combinations thereof. 1. A process for producing chlorotrifluoroethylene (CFO-1113) comprising:dehydrochlorinating 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a) in the presence of a catalyst selected from the group consisting of (i) one or more metal halides; (ii) one or more halogenated metal oxides; (iii) one or more zero-valent metals or metal alloys; (iv) combinations thereof to produce a reaction product comprising CFO-1113.2. The process of wherein the conversion of HCFC-123a is at least about 5 wt. %.3. The process of wherein a selectivity to chlorotrifluoroethylene is at least about 70 wt. %.4. The process of wherein said reaction product comprises less than about 10 wt. % of CFO-1112.5. The process of wherein the dehydrochlorinating step is conducted at a temperature greater than about 400° C.6. The process of wherein a substantial portion of the dehydrochlorinating step is carried out at a temperature of from about 480° C. to about 550° C.7. The process of wherein catalyst comprises a mono-valent metal halide claim 1 , a bi-valent metal halide claim 1 , a tri-valent metal halide claim 1 , or a combination thereof.8. The process of wherein catalyst comprises a mono-valent metal halide claim 1 , a bi-valent metal halide or a combination thereof.9. The process of wherein the catalyst comprises at least one metal halide wherein the component metal is selected from the group consisting of Cr claim 1 , Fe claim 1 , Mg claim 1 , Ca claim 1 , Ni claim 1 , Zn claim 1 , Pd claim 1 , Li claim 1 , Na claim ...

Processes for the Preparation of Silicon Containing Intermetallic Compounds and Intermetallic Compounds Prepared Thereby

Intermetallic compounds, such as metal silicides, e.g., PdSi and/or Pd 2 Si, can be selectively prepared in a two step process including the steps of (1) vacuum impregnating silicon with a metal halide, and (2) ball milling the product of step (1).

One-Step Process for Hexafluoro-2-Butene

Disclosed is a one step process for making of 1,1,1,4,4,4-hexafluoro-2-butene. More specifically, the present invention provides a process for making hexafluoro-2-butene, continuously, from 2-chloro-3,3,3-trifluoropronene using FeO/NiO impregnated carbon catalyst at 600° to 650° C. 1. A process for making 1 ,1 ,1 ,4 ,4 ,4-hexafluoro-2-butene (HFO-1336) from 2-chloro-3 ,3 ,3-trifluoropropene (HCFC-1233xf) comprising reacting HCFC-1233xf with a selected catalyst , at a reactive temperature , to afford HFO-1336.2. The process of claim 1 , which is conducted in the vapor phase.3. The process of claim 2 , which is conducted in a continuous manner.4. The process of claim 2 , wherein the catalyst comprises FeO/NiO.5. The process of claim 4 , wherein the catalyst comprises a ratio of about 95-99 wt % FeOto about 5-1 wt % NiO.6. The process of claim 4 , wherein the catalyst comprises a ratio of about 98 wt % FeOto 2 wt % NiO.7. The process of claim 2 , wherein the catalyst is selected from the group consisting of RuO claim 2 , RuO claim 2 , and OsOin combination with oxides of Pd or Pt.8. The process of claim 2 , wherein the catalyst is impregnated on carbon.9. The process of claim 8 , wherein the carbon is activated carbon.10. The process of claim 9 , wherein the activated carbon is granular with a mesh size of 4-14.11. The process of claim 9 , wherein the activated carbon is pelletized.12. The process of claim 2 , wherein the reaction temperature ranges from 600° to 650° C.13. The process of claim 1 , wherein both the trans and cis isomers of HFO-1336 are formed.14. The process of claim 13 , wherein the predominant isomer of HFO-1336 formed is the trans isomer.15. The process of claim 14 , wherein the ratio of the trans isomer to the cis isomer of HFO-1336 is about 88:12.16. The process of claim 15 , wherein the trans isomer is converted into the cis isomer by reaction with an isomerization catalyst.17. The process of claim 16 , wherein the isomerization catalyst comprises ...

DEHYDROFLUORINATION OF PENTAFLUOROALKANES TO FORM TETRAFLUOROOLEFINS

A method for producing a tetrafluoroolefin, such as 2,3,3,3-tetrafluoropropene (HFO-1234yf), comprises dehydrofluorinating a pentafluoroalkane in a gas phase in the presence of a catalyst comprising chromium oxyfluoride. In a preferred embodiment, 2,3,3,3-tetrafluoropropene (HFO-1234yf) is produced by forming a catalyst comprising chromium oxyfluoride by calcining CrF.xHO, where x is 1-10, in the presence of a flowing gas comprising nitrogen to form a calcined chromium oxyfluoride, and dehydrofluorinating 1,1,1,2,2-pentafluoropropane (HFC-245cb) in a gas phase in the presence of the catalyst to form the 2,3,3,3-tetrafluoropropene (HFO-1234yf). 1. A method for producing 2 ,3 ,3 ,3-tetrafluoropropene (HFO-1234yf) comprising dehydrofluorinating a pentafluoroalkane selected from the group consisting of 1 ,1 ,1 ,2 ,2-pentafluoropropane (HFC-245cb) , 1 ,1 ,1 ,2 ,3-pentafluoropropane (HFC-245eb) and mixtures thereof in a gas phase in the presence of a a chromium oxyfluoride catalyst , containing 0-20 weight % a co-catalyst selected from the group consisting of Zn , Ni , Co , Mn , and Mg.2. A method according to claim 1 , wherein the catalyst comprises a support selected from the group consisting of alumina claim 1 , graphite claim 1 , chromia claim 1 , zirconia claim 1 , titania claim 1 , magnesia claim 1 , activated carbon claim 1 , their corresponding HF-activated compounds claim 1 , and mixtures thereof.3. A method according to claim 1 , wherein the catalyst is formed by calcining CrF.xHO claim 1 , where x is 1-10 claim 1 , in the presence of a flowing gas comprising nitrogen or air to form a calcined chromium oxyfluoride.4. A method according to claim 3 , wherein the catalyst is not activated with hydrogen fluoride.5. A method according to claim 1 , wherein the catalyst is formed by calcining chromium (III) fluoride tetrahydrate.6. A method according to claim 1 , wherein the catalyst is formed by activating CrOwith a mixture of hydrogen fluoride and air claim 1 , to ...

METHOD OF PRODUCING FLUORINE-CONTAINING SULFIDE COMPOUNDS

The present invention aims to provide a method by which fluorine-containing sulfide compounds, particularly sulfide compounds that contain hydrogen and fluorine, can be produced in a simple, low-cost and industrial manner. Provided is a method of producing a fluorine-containing sulfide compound represented by the following formula (2): 16-. (canceled)9. The method of producing a fluorine-containing sulfide compound according to claim 7 , wherein 1.0 to 20.0 equivalents of the fluorinating agent relative to the chlorine-containing sulfide compound is used in terms of the substance's quantitative ratio.10. The method of producing a fluorine-containing sulfide compound according to claim 7 , wherein the reaction is performed at a temperature of 50 to 350° C.11. The method of producing a fluorine-containing sulfide compound according to claim 7 , wherein the chlorine-containing sulfide compound and the fluorinating agent are vaporized before being supplied to a reactor.12. The method of producing a fluorine-containing sulfide compound according to claim 7 , wherein the at least one selected from the group consisting of metal fluorides supported on activated charcoal claim 7 , metal chlorides supported on activated charcoal claim 7 , and metal catalysts supported on activated charcoal is at least one selected from the group consisting of chromium fluoride claim 7 , nickel fluoride claim 7 , copper fluoride claim 7 , silver fluoride claim 7 , sodium fluoride claim 7 , potassium fluoride claim 7 , cesium fluoride claim 7 , chromium chloride claim 7 , nickel chloride claim 7 , chromium claim 7 , copper claim 7 , zinc claim 7 , silver claim 7 , magnesium claim 7 , and titanium claim 7 , all of which is supported on activated charcoal.13. The method of producing a fluorine-containing sulfide compound according to claim 7 , wherein the chlorine-containing sulfide compound is CH-S-CCl claim 7 , and the fluorine-containing sulfide compound is CH-S-CF.14. The method of producing ...

SELECTIVE CATALYTIC DEHYDROCHLORINATION OF HYDROCHLOROFLUOROCARBONS

A dehydrochlorination process is disclosed. The process involves contacting RCHClCHCl with a chromium oxyfluoride catalyst in a reaction zone to produce a product mixture comprising RCCl═CH, wherein Ris a perfluorinated alkyl group. 1. A composition comprising RCCl═CHand a dehydrochlorination catalyst having the formula CrOF , wherein x+y/2=3 , wherein R , is a perfluorination alkyl group.2. The composition according to wherein Ris CF.3. The composition according to wherein Ris CFCF.4. The composition according to wherein HF is additionally present.5. The composition according to wherein an inert gas is additionally present.6. The composition according to wherein the dehydrochlorination catalyst has a surface area of from 10 m/g to 800 m/g.7. The composition according to wherein the dehydrochlorination catalyst contains an alkali metal content of from 2000 parts-per-million or less.8. The composition according to wherein the alkali metal content comprises potassium. This application is a divisional application of U.S. application Ser. No. 16/688,688 filed Nov. 19, 2019, which is a divisional of U.S. application Ser. No. 15/666,770 filed Aug. 2, 2017, which is a continuation of U.S. application Ser. No. 13/397,956 filed Feb. 16, 2012, which claims benefit of U.S. Provisional Application No. 61/444,874 filed Feb. 21, 2011, the entire contents of which are incorporated herein by reference.This disclosure relates in general to the selective catalytic dehydrochlorination of hydrochlorofluorocarbons (HCFCs) to make hydrochlorofluoroolefins (HCFOs). More specifically, the catalyst is a chromium oxyfluoride catalyst.Hydrochlorofluoroolefins (HCFOs), having low ozone depletion potential and low global warming potentials, are regarded as candidates for replacing saturated CFCs (chlorofluorocarbons) and HCFCs (hydrochlorofluorocarbons). HCFOs can be employed in a wide range of applications, including their use as refrigerants, solvents, foam expansion agents, cleaning agents, ...

PROCESS FOR PRODUCING CHLOROTRIFLUOROETHYLENE

The present invention relates, at least in part, to a process for making chlorotrifluoroethylene (CFO-1113) from 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a). In certain aspects, the process includes dehydrochlorinating 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a) in the presence of a catalyst selected from the group consisting of (i) one or more metal halides; (ii) one or more halogenated metal oxides; (iii) one or more zero-valent metals or metal alloys; (iv) combinations thereof. 1. A process for producing chlorotrifluoroethylene (CFO-1113) comprising: dehydrochlorinating 1 ,2-dichloro-1 ,1 ,2-trifluoroethane (HCFC-123a) in the presence of a catalyst selected from the group consisting of (i) one or more metal halides; (ii) one or more halogenated metal oxides; (iii) one or more zero-valent metals or metal alloys; (iv) combinations thereof to produce a reaction product comprising CFO-1113.2. The process of wherein the conversion of HCFC-123a is at least about 5 wt. % claim 1 , the selectivity to chlorotrifluoroethylene is at least about 70 wt. % claim 1 , and said reaction product comprises less than about 10 wt. % of CFO-1112.3. (canceled)4. (canceled)5. (canceled)6. The process of wherein a substantial portion of the dehydrochlorinating step is carried out at a temperature of from about 480° C. to about 550° C.7. The process of wherein catalyst comprises a mono-valent metal halide claim 1 , a bi-valent metal halide claim 1 , a tri-valent metal halide claim 1 , or a combination thereof.8. The process of wherein catalyst comprises a mono-valent metal halide claim 1 , a bi-valent metal halide or a combination thereof.9. The process of wherein the catalyst comprises at least one metal halide wherein the component metal is selected from the group consisting of Cr claim 1 , Fe claim 1 , Mg claim 1 , Ca claim 1 , Ni claim 1 , Zn claim 1 , Pd claim 1 , Li claim 1 , Na claim 1 , K claim 1 , and Cs claim 1 , and the component halogen is selected from the group ...

METHOD FOR PREPARING METAL FLUORIDE CATALYSTS AND DEHYDROFLUORINATION METHOD USING THE SAME

Disclosed is a method for preparing a metal fluoride catalyst as a dehydrofluorination catalyst having high activity under a mild condition using a trifluoroacetic acid solution with no use of HF gas having fluidity and corrosive property. Disclosed also is a dehydrofluorination method for preparing HFO-1225ye from HFP-236ea by using the catalyst with high efficiency. 1. A method for preparing a metal fluoride catalyst , comprising adding a trifluoroacetic acid solution to a metal precursor to form a metal fluoride catalyst.2. The method for preparing a metal fluoride catalyst according to claim 1 , wherein the metal precursor is a chromium precursor.3. The method for preparing a metal fluoride catalyst according to claim 2 , wherein the chromium precursor is chromium oxide obtained by a sol-gel process.4. The method for preparing a metal fluoride catalyst according to claim 2 , wherein the chromium precursor is in the form of wet gel.5. The method for preparing a metal fluoride catalyst according to claim 2 , wherein the trifluoroacetic acid solution is a solution of trifluoroacetic acid dissolved in water claim 2 , ethanol or dioxane.6. The method for preparing a metal fluoride catalyst according to claim 2 , wherein the trifluoroacetic acid solution has a concentration of 0.001-0.1M.7. A metal fluoride catalyst obtained by the method as defined in .8. A dehydrofluorination method comprising:introducing 1,1,2,3,3,3-hexafluoropropane into a reactor; and{'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'adding the metal fluoride catalyst obtained by the method as defined in to the reactor to obtain 1,2,3,3,3-pentafluoropropene.'}9. The dehydrofluorination method according to claim 8 , wherein the reactor has a temperature of 300-500° C. when preparing 1 claim 8 ,2 claim 8 ,3 claim 8 ,3 claim 8 ,3-pentafluoropropene.10. The dehydrofluorination method according to claim 8 , wherein the metal fluoride catalyst is a chromium fluoride catalyst. This application claims ...

METHOD FOR REDUCING CARBON DEPOSITS ON CATALYST IN RECYCLING HFC-23

Disclosed is a method for reducing carbon deposits on a catalyst in recycling HFC-23. The recycling is realized by means of a fluorine-chlorine exchange reaction with HFC-23 and a halogenated hydrocarbon. The catalyst for the fluorine-chlorine exchange reaction comprises a main body catalyst and a precious metal. The precious metal is selected from at least one of Pt, Pd, Ru, Au or Rh, and has an addition amount of 0.01-2 wt %. During the fluorine-chlorine exchange reaction, hydrogen gas is introduced. The invention has advantages of good catalyst stability, long life, etc. 1. A method for reducing carbon deposits on a catalyst in recycling HFC-23 , the recycling is realized by means of a fluorine-chlorine exchange reaction with HFC-23 and a halogenated hydrocarbon , wherein the catalyst for the fluorine-chlorine exchange reaction comprises a main body catalyst and a precious metal , the precious metal is selected from at least one of Pt , Pd , Ru , Au or Rh , and has an addition amount of 0.01-2 wt %;during the fluorine-chlorine exchange reaction, hydrogen gas is introduced.2. The method for reducing carbon deposits on a catalyst in recycling HFC-23 according to claim 1 , wherein the precious metal is Pt or Pd claim 1 , and has an addition amount of 0.1-0.5 wt %.3. The method for reducing carbon deposits on a catalyst in recycling HFC-23 according to claim 1 , wherein the catalyst further comprises a metal oxide claim 1 , and the metal oxide is selected at least one metal oxide of K claim 1 , Na claim 1 , Fe claim 1 , Co claim 1 , Cu claim 1 , Ni claim 1 , Zn or Ti claim 1 , and has an addition amount of 0.1-5 wt %.4. The method for reducing carbon deposits on a catalyst in recycling HFC-23 according to claim 3 , wherein the metal oxide is selected from metal oxides of Fe claim 3 , Co claim 3 , Ni or Zn claim 3 , and has an addition amount of 0.5 -2 wt %.5. The method for reducing carbon deposits on a catalyst in recycling HFC-23 according to claim 1 , wherein ...

Use of Novel catalyst and method for treating PCB inked polymer waste by the novel catalyst

A novel catalyst, a use thereof and a method for treating PCB inked waste by using the same are disclosed. The catalyst of the present disclosure is represented by the following formula (I): 1. A catalyst , representing by the following formula (I):{'br': None, 'sub': 'a', 'sup': m+', 'n−, '[M(O)]X\u2003\u2003(I)'}wherein M is an element of Group IB, Group IVB, Group VB, Group VIB, Group VIIB or Group VIIIB;{'sub': 2', 'n', '3', '12', '25', '2', '6', '4', '2', 'n', '4', '3', '2', '25, 'X is Cl, Br, I, OAc, OC(O)(CF)CF, OC(O)CH, [(OSOCH-CHCH)], OTf, OTs, SO, SOC Hor acetylacetonate (acac);'}a is an integral of 0 to 3;m is an integral of 2 to 4; andn is an integral of 1 or 2.2. The catalyst of claim 1 , wherein a is 0 claim 1 , and M is Ti claim 1 , Zr claim 1 , Hf claim 1 , V claim 1 , Fe claim 1 , Cu or Mn.3. The catalyst of claim 1 , wherein M(O)is VO claim 1 , VO claim 1 , ZrO claim 1 , HfO claim 1 , WO claim 1 , MoO claim 1 , CrOor ReO.4. A use of a catalyst for degrading inks or acylating or recycling polymers claim 1 , wherein the catalyst is representing by the following formula (I):{'br': None, 'sub': 'a', 'sup': m+', 'n−, '[M(O)]X\u2003\u2003(I)'}wherein M is an element of Group IB, Group IVB, Group VB, Group VIB, Group VIIB or Group VIIIB;{'sub': 2', 'n', '3', '12', '25', '2', '6', '4', '2', 'n', '4', '3', '12', '25, 'X is Cl, Br, I, OAc, OC(O)(CF)CF, OC(O)CH, [(OSOCH-CHCH)], OTf, OTs, SO, SOCHor acetylacetonate (acac);'}a is an integral of 0 to 3;m is an integral of 2 to 4; andn is an integral of 1 or 2.5. A method for treating a PCB inked polymer waste claim 1 , comprising the following steps: {'br': None, 'sub': 'a', 'sup': m+', 'n−, '[M(O)]X\u2003\u2003(I)'}, 'mixing a PCB inked polymer waste, a catalyst representing by the following formula (I), a reagent and a first solvent to obtain a mixturewherein M is an element of Group IB, Group IVB, Group VB, Group VIB, Group VIIB or Group VIIIB;{'sub': 2', 'n', '3', '12', '25', '2', '6', '4', '2', 'n', '4', '3 ...

Selective catalytic dehydrochlorination of hydrchlorofluorocarbons

A dehydrochlorination process is disclosed. The process involves contacting RfCHClCH2Cl with a chromium oxyfluoride catalyst in a reaction zone to produce a product mixture comprising RfCCl═CH2, wherein Rf is a perfluorinated alkyl group.

Method for Producing 1,2-Dichloro-3,3,3-Trifluoropropene

A method for producing 1,2-dichloro-3,3,3-trifluoropropene according to the present invention includes the step of reacting 1,1,2,3,3-pentachloropropene with a fluorinating agent where hydrogen fluoride is used as the fluorinating agent. 135.-. (canceled)36. A method for producing 1 ,2-dichloro-3 ,3 ,3-trifluoropropene by fluorinating 1 ,1 ,2 ,3 ,3-pentachloropropene by a reaction with a fluorinating agent , wherein hydrogen fluoride is used as the fluorinating agent.37. The method according to claim 36 , wherein the reaction is conducted in a liquid phase.38. The method according to claim 36 , wherein the reaction is conducted in a gas phase.39. The method according to claim 36 , wherein usage of the hydrogen fluoride is 3 to 40 mol relative to 1 mol of 1 claim 36 ,1 claim 36 ,2 claim 36 ,3 claim 36 ,3-pentachloropropene.40. The method according to claim 37 , wherein the reaction is conducted at 100 to 200° C.41. The method according to claim 37 , wherein the reaction is conducted at 140 to 180° C.42. The method according to claim 38 , wherein the reaction is conducted at 160 to 600° C.43. The method according to claim 36 , wherein the reaction is conducted in the absence or presence of catalyst.44. The method according to claim 43 , wherein the reaction is conducted by using a catalyst that is a metal oxide claim 43 , a metal fluoride or a metal compound-supported catalyst and that the catalyst is optionally subjected to a fluorination treatment to be used in the reaction.45. The method according to claim 36 , wherein the reaction is conducted in the presence of at least one selected from the group consisting of chlorine claim 36 , oxygen and air.46. The method according to claim 36 , wherein the reaction is conducted in the absence of solvent.47. The method according to claim 36 , wherein 1 claim 36 ,2 claim 36 ,3-trichloro-3 claim 36 ,3-difluoropropene claim 36 , together with 1 claim 36 ,2-dichloro-3 claim 36 ,3 claim 36 ,3-trifluoropropene claim 36 , is formed ...

ELECTROCHEMICAL HYDROXIDE SYSTEMS AND METHODS USING METAL OXIDATION

There are provided methods and systems for an electrochemical cell including an anode and a cathode where the anode is contacted with a metal ion that converts the metal ion from a lower oxidation state to a higher oxidation state. The metal ion in the higher oxidation state is reacted with hydrogen gas, an unsaturated hydrocarbon, and/or a saturated hydrocarbon to form products. 128-. (canceled)29. A method , comprising:contacting an anode with an anode electrolyte in an electrochemical cell wherein the anode electrolyte comprises saltwater and metal halide;contacting a cathode with a cathode electrolyte in the electrochemical cell;applying a voltage to the anode and the cathode and oxidizing the metal halide from a lower oxidation state to a higher oxidation state at the anode; andhalogenating an unsaturated hydrocarbon or a saturated hydrocarbon with the anode electrolyte comprising the metal halide in the higher oxidation state in an aqueous medium to result in a halohydrocarbon and the metal halide in the lower oxidation state.301. The method of claim , further comprising forming an alkali , water , or hydrogen gas at the cathode.311. The method of claim , wherein the cathode electrolyte comprises water and the cathode is an oxygen depolarizing cathode that reduces oxygen and water to hydroxide ions; the cathode electrolyte comprises water and the cathode is a hydrogen gas producing cathode that reduces water to hydrogen gas and hydroxide ions; the cathode electrolyte comprises hydrochloric acid and the cathode is a hydrogen gas producing cathode that reduces hydrochloric acid to hydrogen gas; or the cathode electrolyte comprises hydrochloric acid and the cathode is an oxygen depolarizing cathode that reacts hydrochloric acid and oxygen gas to form water.321. The method of claim , wherein metal ion in the metal halide is selected from the group consisting of iron , chromium , copper , tin , silver , cobalt , uranium , lead , mercury , vanadium , bismuth , ...

Ethylene selective oligomerization catalyst systems and method for ethylene oligomerization using the same

The disclosure provides a catalyst system and a method for ethylene oligomerization using this. The catalyst system contains: ligand a, containing carbene groups of imidazole ring type; transition metal compound b, that is one of IVB˜VIII group metal compounds; activator c, that is a compound containing III A group metals; the ligand a contains at least one group as shown in general formula I: 2. The catalyst system according to claim 1 , wherein the first heteroatom is selected from silicon claim 1 , tin claim 1 , boron claim 1 , phosphorus claim 1 , nitrogen claim 1 , oxygen or sulfur.3. The catalyst system according to claim 1 , wherein the main chain of the bridging group A includes —(CH)— (1≤n≤8); phenyl; biphenyl; naphthyl; anthryl or —(CH)—SiR′R″—(CH)(0≤n≤3 claim 1 , 0≤m≤3) claim 1 , in which R′ and R″ are each independently methyl claim 1 , isopropyl claim 1 , cyclohexanyl claim 1 , cyclopentyl claim 1 , phenyl claim 1 , naphthyl or 2 claim 1 ,6-diisopropylphenyl respectively.4. The catalyst system according to claim 2 , wherein the main chain of the bridging group A includes —(CH)— (1≤n≤8); phenyl; biphenyl; napthyl; anthryl or —(CH)—SiR′R″—(CH)(0≤n≤3 claim 2 , 0≤m≤3) claim 2 , in which R′ and R″ are each independently methyl claim 2 , isopropyl claim 2 , cyclohexanyl claim 2 , cyclopentyl claim 2 , phenyl claim 2 , naphthyl or 2 claim 2 ,6-diisopropyl phenyl claim 2 , respectively.5. The catalyst system according to claim 1 , wherein the second heteroatom is selected from phosphorous claim 1 , nitrogen claim 1 , sulfur or oxygen.6. The catalyst system according to claim 1 , wherein E in general formula I contains alkyl phosphino claim 1 , aryl phosphino claim 1 , alkyl aryl phosphino claim 1 , alkyl amino claim 1 , aryl amino claim 1 , mercapto claim 1 , and preferably diisopropyl phosphino claim 1 , dicyclohexyl phosphino claim 1 , dimethyl phosphino claim 1 , diethyl phosphino claim 1 , diphenyl phosphino claim 1 , di-o-methylbenzene phosphino claim 1 , ...

CARBIDE-DERIVED CARBONS HAVING INCORPORATED METAL CHLORIDE OR METALLIC NANOPARTICLES

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

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

The present invention relates to a process for the gas-phase production of 2,3,3,3-tetrafluoropropene, comprising the steps: i) providing a composition A comprising 2-chloro-3,3,3-trifluoropropene and/or 2,3-dichloro-1,1,1-trifluoropropane and/or 2-chloro-1,1,1,2-tetrafluoropropane or a composition B comprising 1,1,1,2,2-pentafluoropropane and/or 1,1,1,2,3-pentafluoropropane; ii) placing said composition A in contact with hydrofluoric acid in the presence of a catalytic composition comprising a chromium-based catalyst or placing said composition B in contact with a catalytic composition comprising a chromium-based catalyst to produce a composition C comprising 2,3,3,3-tetrafluoropropene, characterized in that step ii) is performed at a temperature of between 310° C. and 450° C. and in that the temperature of step ii) is controlled so as not to exceed 450° C.; and when said catalyst is deactivated, the temperature of step ii) is increased in increments from 0.5° C. to 20° C. on condition that the temperature does not exceed 450° C. 17-. (canceled)8. A process for the gas-phase production of 2 ,3 ,3 ,3-tetrafluoropropene , comprising the steps:i. providing a composition A comprising 2-chloro-3,3,3-trifluoropropene and/or 2,3-dichloro-1,1,1-trifluoropropane and/or 2-chloro-1,1,1,2-tetrafluoropropane or a composition B comprising 1,1,1,2,2-pentafluoropropane and/or 1,1,1,2,3-pentafluoropropane;ii. placing said composition A in contact with hydrofluoric acid in the presence of a catalytic composition comprising a chromium-based catalyst or placing said composition B in contact with a catalytic composition comprising a chromium-based catalyst to produce a composition C comprising 2,3,3,3-tetrafluoropropene, wherein step ii) is performed at a temperature of between 310° C. and 450° C. and the temperature of step ii) is controlled so as not to exceed 450° C.; and when said catalyst is deactivated, the temperature of step ii) is increased in increments from 0.5° C. to 20° C. ...

PREPARATION OF DIESTERS OF (METH)ACRYLIC ACID FROM EPOXIDES

The invention relates to a method for preparation of diesters from anhydrides of carboxylic acids. 115-. (canceled)17. The process of claim 16 , wherein:{'sup': 1', '2, 'Ris a hydrogen atom, Ris a vinyl group, and the (meth)acrylic anhydride of formula (II) is acrylic acid anhydride; or alternatively{'sup': 1', '2, 'Ris a methyl group, Ris a 1-methylvinyl group and the (meth)acrylic anhydride of formula (II) is methacrylic acid anhydride.'}18. The process of claim 16 , wherein the optionally substituted aliphatic or aromatic substituents having up to 17 carbon atoms are selected from the group consisting of: optionally substituted alkyl claim 16 , cycloalkyl claim 16 , alkenyl claim 16 , or alkadienyl substituents having up to 17 carbon atoms optionally substituted with one substituent Rselected from: a halogen atom claim 16 , —CN claim 16 , —SCN claim 16 , —OCN claim 16 , and —NCO.19. The process of claim 16 , wherein the epoxide of general Formula (III) is selected from the group consisting of: ethylene oxide; propylene oxide; 1-hexene oxide; cyclohexene oxide; cyclopentene oxide; 1-butene oxide; 2-butene oxide; isobutene oxide; styrene oxide; and glycidyl methacrylate.20. The process of claim 16 , wherein process step (a) is carried out in the presence of the first catalyst claim 16 , the second catalyst and the co-catalyst.21. The process of claim 16 , wherein the co-catalyst is a quaternary ammonium salt.22. The process of claim 16 , wherein the co-catalyst is selected from the group consisting of: tetrabutylammonium chloride; tetrabutylammonium bromide; tetraethylammonium chloride; tetrabutylammonium acetate; tetramethylammonium chloride; tetrapentylammonium bromide; cetyl-trimethylammonium bromide; 1-butyl-3-methyl-imidazolyl chloride; cetylpyridinium chloride; and triethylbenzylammonium chloride.23. The process of claim 16 , wherein the second catalyst is a chromium (III) carboxylate.24. The process of claim 23 , wherein the chromium (III) carboxylate is ...

Gas-phase catalytic fluorination with chromium catalysts

A process for the fluorination of a chlorinated C3 alkane or alkene compound having at least one chlorine atom into a fluorinated C3 alkane or alkene compound having at least one fluorine atom includes the following steps: a) contacting, in a reactor, the chlorinated compound with hydrogen fluoride in gas phase in the presence of a fluorination catalyst to produce a fluorinated compound, and b) regenerating the fluorination catalyst used in step a). The step (b) of regenerating the fluorination catalyst comprises (c) the treatment of said fluorination catalyst with an oxidizing agent-containing gas flow to form an oxidized fluorination catalyst, and (d) the treatment of the oxidized fluorination catalyst obtained in step (c) with a gaseous mixture comprising a reducing agent and an inert gas. The catalyst regenerated in step b) is reused in step a) and the reducing agent is selected from C-Chydrohalocarbons. 1. Process for the fluorination of a chlorinated C3 alkane or alkene compound having at least one chlorine atom into a fluorinated C3 alkane or alkene compound having at least one fluorine atom comprising the following steps:a. contacting, in a reactor, the chlorinated compound with hydrogen fluoride in gas phase in the presence of a fluorination catalyst to produce a fluorinated compound, andb. regenerating the fluorination catalyst used in step a),{'sub': 1', '10, 'wherein the step (b) of regenerating the fluorination catalyst comprises (c) the treatment of said fluorination catalyst with an oxidizing agent-containing gas flow to form an oxidized fluorination catalyst, and (d) the treatment of the oxidized fluorination catalyst obtained in step (c) with a gaseous mixture comprising a reducing agent and an inert gas; the catalyst regenerated in step b) being reused in step a) and the reducing agent being selected from the group consisting of C-Chydrohalocarbons.'}2. Process for the fluorination of a chlorinated C3 alkane or alkene compound having at least one ...

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

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

METHOD OF SELECTIVELY OXIDIZING LIGNIN

A method of selectively reacting lignin or a lignin-derived reactant to yield an aromatic product. The method includes the step of reacting lignin or a lignin-derived reactant with a molybdenum-containing catalyst, in a solvent, and optionally in the presence of an oxidant, for a time and a temperature wherein at least a portion of the lignin or lignin-derived reactant is selectively converted into an aromatic product, preferably coniferaldehyde and/or sinapaldehyde. 1. A method of selectively reacting lignin or a lignin-derived reactant to yield an aromatic product , the method comprising:reacting lignin or a lignin-derived reactant with a molybdenum-containing catalyst, in a solvent, for a time and at a temperature wherein at least a portion of the lignin or lignin-derived reactant is selectively converted into an aromatic product.2. The method of claim 1 , wherein the molybdenum-containing catalyst is selected from the group consisting of MoOCl(DMSO) claim 1 , MoO claim 1 , NaMoO.2HO claim 1 , MoOCl claim 1 , [CHMo(CO)] claim 1 , and Mo(dppf)(CO).3. The method of claim 1 , wherein the lignin or a lignin-derived reactant is reacted at a temperature of from 120° C. to 250° C.4. The method of claim 1 , wherein the lignin or a lignin-derived reactant is reacted at a temperature of from 120° C. to 200° C.5. The method of claim 1 , wherein the lignin or a lignin-derived reactant is reacted at a temperature of from 120° C. to 160° C.6. The method of claim 1 , in which the temperature is established by microwave irradiation.7. The method of claim 1 , in which the temperature is established by radiant heating.8. The method of claim 1 , wherein the solvent is selected from the group consisting of dimethyl sulfoxide (DMSO) claim 1 , gamma-valerolactone (GVL) claim 1 , dimethylformamide (DMF) claim 1 , and cyclohexanone.9. The method of claim 1 , wherein the solvent is DMSO claim 1 , and the lignin or a lignin-derived reactant is reacted with the molybdenum-containing ...

Methods For Making Fluorided Chromium (VI) Catalysts, And Polymerization Processes Using the Same

Methods for preparing a fluorided chromium catalyst can include a step of calcining a supported chromium catalyst at a peak calcining temperature to produce a calcined supported chromium catalyst, followed by contacting the calcined supported chromium catalyst at a peak fluoriding temperature with a vapor comprising a fluorine-containing compound to produce the fluorided chromium catalyst. The peak fluoriding temperature can be at least 50° C. less, and often from 200° C. to 500° C. less, than the peak calcining temperature. Polymers produced using the fluorided chromium catalyst can have a beneficial combination of higher melt index, narrower molecular weight distribution, and lower long chain branch content.

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

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

CHROMIUM OXYFLUORIDE CATALYSTS HAVING HIGH FLUORINATION ACTIVITY

X-Ray photoelectron spectroscopy (XPS) is used to assess or predict the catalytic activity of a chromium oxyfluoride catalyst in a reaction wherein a chlorinated compound is converted to a fluorinated compound. 1. A chromium oxyfluoride catalyst active for fluorination of a chlorinated compound , wherein the chromium oxyfluoride catalyst is comprised of a first chromium species and a second chromium species , wherein the first chromium species exhibits a first X-ray photoelectron spectroscopy (XPS) chromium Cr 2ppeak between 576.9 eV+/−0.2 eV and 578.0 eV+/−0.2 eV and the second chromium species exhibits a second X-ray photoelectron spectroscopy (XPS) chromium Cr 2p/2 peak between 580.0 eV+/−0.2 eV and 581.4 eV+/−0.2 eV and wherein the intensity of the second XPS chromium peak is greater than the intensity of the first XPS chromium peak.2. The chromium oxyfluoride catalyst of claim 1 , wherein the chromium oxyfluoride catalyst is a supported catalyst.3. The chromium oxyfluoride catalyst of claim 1 , wherein the chromium oxyfluoride catalyst is a catalyst supported on an aluminum-containing support.4. The chromium oxyfluoride catalyst of claim 2 , wherein the ratio of the intensity of the second XPS chromium peak to the intensity of the first XPS chromium peak is greater than 2.5.5. The chromium oxyfluoride catalyst of claim 1 , wherein the chromium oxyfluoride catalyst is a bulk catalyst.6. The chromium oxyfluoride catalyst of claim 5 , wherein the ratio of the intensity of the second XPS chromium peak to the intensity of the first XPS chromium peak is greater than 8.0.7. The chromium oxyfluoride catalyst of claim 1 , wherein the chromium oxyfluoride catalyst is comprised of a first oxygen species and a second oxygen species claim 1 , wherein the first oxygen species exhibits a first X-ray photoelectron spectroscopy (XPS) oxygen O 1s peak between 530.3 eV+0.2 eV and 531.6 eV±0.2 eV and the second oxygen species exhibits a second X-ray photoelectron spectroscopy (XPS ...

Catalytic isomerization of z-1,1,1,4,4,4-hexafluoro-2-butene to e-1,1,1,4,4,4-hexafluoro-2-butene

A process is disclosed for (i) producing E-1,1,1,4,4,4-hexafluoro-2-butene (E-HFO-1336mzz) from Z-1,1,1,4,4,4-hexafluoro-2-butene (Z-HFO-1336mzz), comprising the steps of (a) providing a starting material comprising Z-1,1,1,4,4,4-hexafluoro-2-butene, (b) contacting the starting material with a suitable catalyst in a reaction zone to produce E-HFO-1336mzz; and optionally, (c) recovering the E-HFO-1336mzz. The process may be performed in the gas phase or in the liquid phase and as a batch process or as a continuous process.

METHOD FOR PRODUCING DIFLUOROETHYLENE

The present invention aims to provide an efficient method for obtaining a desired isomer of HFO-1132 from a composition comprising trans-1,2-difluoroethylene (HFO-1132(E)) and cis-1,2-difluoroethylene (HFO-1132(Z)). 1. A method for producing trans-1 ,2-difluoroethylene (HFO-1132(E)) and/or cis-1 ,2-difluoroethylene (HFO-1132(Z)) , comprising the step of:(1) supplying a composition comprising HFO-1132(E) and/or HFO-1132(Z) to a reactor filled with a catalyst to perform an isomerization reaction between the HFO-1132(E) and the HFO-1132(Z).2. A method for producing cis-1 ,2-difluoroethylene (HFO-1132(Z)) , comprising the step of:(1A) supplying trans-1,2-difluoroethylene (HFO-1132(E)) or a composition comprising HFO-1132(E) and HFO-1132(Z) to a reactor filled with a catalyst to perform an isomerization reaction between the HFO-1132(E) and the HFO-1132(Z).3. A method for producing HFO-1132(E) , comprising the step of:(1B) supplying HFO-1132(Z) or a composition comprising HFO-1132(E) and HFO-1132(Z) to a reactor filled with a catalyst to perform an isomerization reaction between the HFO-1132(E) and the HFO-1132(Z).4. The production method according to any one of to , the reaction product obtained in step (1), (1A), or (1B) comprises HFO-1132(E) and HFO-1132(Z), and', 'the method further comprises steps (2) and (3):, 'wherein'}(2) separating the reaction product obtained in step (1), (1A), or (1B) into a first stream comprising the HFO-1132(E) as a main component, and a second stream comprising the HFO-1132(Z) as a main component; and(3) recycling the first stream or the second stream obtained in step (2) to the reactor, to subject the first stream or the second stream to the isomerization reaction.5. The production method according to any one of to , further comprising the step of:(i) subjecting a halogenated ethane to a dehydrohalogenation reaction or a dehalogenation reaction to obtain a composition comprising HFO-1132(E) and HFO-1132(Z), 'the composition comprising HFO ...

CATALYST AND PROCESS USING THE CATALYST FOR MANUFACTURING FLUORINATED HYDROCARBONS

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

CATALYTIC CHLORINATION OF 3,3,3-TRIFLUOROPROPENE TO 2,3-DICHLORO-1,1,1-TRIFLUOROPROPANE

The present invention relates to a process for preparing 1,1,1-trifluoro-2,3-dichloropropane which comprises contacting chlorine with 3,3,3-trifluoropropene in the presence of a catalyst to form 1,1,1-trifluoro-2,3-dichloropropane, wherein the catalyst comprises at least one metal halide, where the metal is a metal from Group 13, 14 or 15 of the periodic table or a transition metal or combination thereof. 141-. (canceled)42. A composition comprising chlorine , 3 ,3 ,3-trifluoropropene and a catalyst , wherein the catalyst comprises at least one metal halide , where the metal is a metal from Group 13 , 14 or 15 of the periodic table or a transition metal or combination thereof and the metal halide is supported on activated carbon.43. The composition according to wherein the activated carbon may optionally be acid washed or caustic washed.44. The composition according to wherein the metal is nickel claim 42 , chromium claim 42 , iron claim 42 , scandium claim 42 , yttrium claim 42 , lanthanum claim 42 , titanium claim 42 , zirconium claim 42 , hafnium claim 42 , vanadium claim 42 , molybdenum claim 42 , tungsten claim 42 , manganese claim 42 , rhenium claim 42 , ruthenium claim 42 , osmium claim 42 , cobalt claim 42 , palladium claim 42 , copper claim 42 , zinc claim 42 , tantalum claim 42 , aluminum claim 42 , tin claim 42 , or lead.45. The composition according to herein the metal halide is nickel halide claim 42 , iron halide or chromium halide.46. The composition according to wherein the halide is a chloride.47. The composition according to wherein the metal halide is nickel chloride claim 42 , iron halide or chromium halide.48. The composition according to wherein the mole ratio of 3 claim 42 ,3 claim 42 ,3-trifluoropropane to chlorine ranges from about 1:0.02 to about 1:1.49. The composition according to wherein the mole ratio of 3 claim 48 ,3 claim 48 ,3-trifluoropropene to chlorine ranges from about 1:0.1 to about 1:0.8.50. The composition according to wherein ...

Hydrogenation catalyst, its production and application thereof

The present application relates to a hydrogenation catalyst, a process for producing the same and application thereof in the hydrotreatment of feedstock oil. The process comprises at least the following steps: (1) contacting a first active metal component and a first organic complexing agent with a carrier to obtain a composite carrier; (2) calcining the composite carrier to obtain a calcined composite carrier having a total carbon content of 1% by weight or less; and (3) contacting a second organic complexing agent with the calcined composite carrier to obtain the hydrogenation catalyst. The hydrogenation catalyst has both excellent hydrodesulfurization activity and hydrodenitrogenation activity, and exhibits a significantly prolonged service life. 117-. (canceled)18. A process for producing a hydrogenation catalyst , comprising the steps of:(1) contacting a first active metal component, a first organic complexing agent and an optional coagent with a carrier to obtain a composite carrier;(2) calcining the composite carrier to obtain a calcined composite carrier, wherein the total carbon content on dry basis of the calcined composite carrier is 1% by weight or less, 0.5% by weight or less, 0.4% by weight or less, 0.3% by weight or less, 0.1% by weight or less, 0.08% by weight or less, 0.06% by weight or less, 0.04% by weight or less, 0.03% by weight or less, 0.01% by weight or less, or 0.005% by weight or less, based on the dry weight of the calcined composite carrier; and(3) contacting a second organic complexing agent with the calcined composite carrier to obtain the hydrogenation catalyst, andoptionally, the process further comprises one or more of the following steps:(0) producing the carrier; and(4) sulfurizing the hydrogenation catalyst.19. The process according to claim 18 , wherein the step (0) further comprises the following steps:(0-1) forming a carrier precursor or a carrier precursor composition to obtain a preformed carrier, wherein the carrier ...

Metal hydroxide based ionic liquid composition

The present disclosure envisages an ionic liquid composition comprising at least one metal hydroxide; at least one metal halide; and at least one solvent. Also envisaged is a process for preparing an ionic liquid composition. The process comprises mixing in a reaction vessel, at least one metal hydroxide and at least one metal halide in the presence of at least one solvent under a nitrogen atmosphere and continuous stirring followed by cooling under continuous stirring to obtain the ionic liquid composition.

METHOD FOR PREPARING 2,3,3,3-TETRAFLUOROPROPENE

Provided are a fluorination catalyst for preparing 2,3,3,3-tetrafluoropropene and a method using the catalyst for preparing 2,3,3,3-tetrafluoropropene. The catalyst has the following structural formula: Crx(Y,Z)OF, where Y is one or a combination of two or more among Al, Zn, and Mg, and where Z is a rare earth element having an oxygen-storing/releasing function. The catalyst has in preparing 2,3,3,3-tetrafluoropropene the advantages of increased raw material conversion rate, great product selectivity, and extended catalyst service life. 1. A fluorination catalyst for preparing 2 ,3 ,3 ,3-tetrafluoropropene , characterized in that the fluorination catalyst has the following formula (I):{'br': None, 'sub': 1', '0.005-0.5', '0.1-10', '1.0-3.0, 'Cr(Y,Z)OF\u2003\u2003(I)'}wherein Y is selected from Al, Zn, Mg, or a combination thereof, and Z is a rare earth element capable of storing/releasing oxygen.2. The fluorination catalyst for preparing 2 claim 1 ,3 claim 1 ,3 claim 1 ,3-tetrafluoropropene according to claim 1 , characterized in that the rare earth element is selected from Ce claim 1 , La claim 1 , Pr claim 1 , or a combination thereof.3. The fluorination catalyst for preparing 2 claim 1 ,3 claim 1 ,3 claim 1 ,3-tetrafluoropropene according to claim 1 , characterized in that the fluorination catalyst was prepared by a process claim 1 , in which a fluorine-containing surfactant was added.4. The fluorination catalyst for preparing 2 claim 3 ,3 claim 3 ,3 claim 3 ,3-tetrafluoropropene according to claim 3 , characterized in that the fluorine-containing surfactant is perfluorooctylsulfonyl fluoride or a soluble salt of perfluorooctylsulfonic acid.5. A method for preparing 2 claim 1 ,3 claim 1 ,3 claim 1 ,3-tetrafluoropropene claim 1 , comprising: reacting 2-chloro-3 claim 1 ,3 claim 1 ,3-trifluoropropene as a starting material with anhydrous hydrogen fluoride claim 1 , under catalysis of the fluorination catalyst of and in the presence of Oand/or O claim 1 , to produce ...

ELECTROCHEMICAL HYDROXIDE SYSTEMS AND METHODS USING METAL OXIDATION

There are provided methods and systems for an electrochemical cell including an anode and a cathode where the anode is contacted with a metal ion that converts the metal ion from a lower oxidation state to a higher oxidation state. The metal ion in the higher oxidation state is reacted with hydrogen gas, an unsaturated hydrocarbon, and/or a saturated hydrocarbon to form products. 150-. (canceled)51. A method , comprising:contacting an anode with an anode electrolyte in an electrochemical cell wherein the anode electrolyte comprises sodium bromide and metal bromide;contacting a cathode with a cathode electrolyte in the electrochemical cell;applying a voltage to the anode and the cathode and oxidizing the metal bromide from a lower oxidation state to a higher oxidation state at the anode; andbrominating an unsaturated hydrocarbon or a saturated hydrocarbon with the anode electrolyte comprising the metal bromide in the higher oxidation state in an aqueous medium to result in a bromohydrocarbon and the metal bromide in the lower oxidation state.52. The method of claim 51 , further comprising forming an alkali claim 51 , water claim 51 , or hydrogen gas at the cathode.53. The method of claim 51 , wherein the cathode electrolyte comprises water and the cathode is an oxygen depolarizing cathode that reduces oxygen and water to hydroxide ions; or the cathode electrolyte comprises water and the cathode is a hydrogen gas producing cathode that reduces water to hydrogen gas and hydroxide ions.54. The method of claim 51 , wherein metal ion in the metal bromide is selected from the group consisting of iron claim 51 , chromium claim 51 , copper claim 51 , tin claim 51 , silver claim 51 , cobalt claim 51 , uranium claim 51 , lead claim 51 , mercury claim 51 , vanadium claim 51 , bismuth claim 51 , titanium claim 51 , ruthenium claim 51 , osmium claim 51 , europium claim 51 , zinc claim 51 , cadmium claim 51 , gold claim 51 , nickel claim 51 , palladium claim 51 , platinum claim 51 ...

CATALYST PREPARED BY REACTIVE MILLING

A process for preparing a catalyst, including the reactive milling of a first reagent, which is a chromium oxide compound, with a second reagent, which is a compound of the formula MM′OF, M and M′ each being an element having an oxidation state greater than or equal to 0, z being from 0 to 1, x being from 0 to 3, y being from 0 to 6, and 2x+y being greater than 0 and less than or equal to 6. 1. A process for preparing a catalyst , comprising the reactive milling of a first reagent , which is a chromium oxide compound , with a second reagent , which is a compound of formula MM′OF , M and M′ each being an element having an oxidation state greater than or equal to 0 , z being from 0 to 1 , x being from 0 to 3 , y being from 0 to 6 , and 2x+y being greater than 0 and less than or equal to 6.2. The process as claimed in claim 1 , wherein the catalyst comprises chromium having an oxidation state of between 3 and 5.3. The process as claimed in claim 1 , wherein the first reagent is chosen from CrO claim 1 , CrO claim 1 , CrOand combinations thereof.4. The process as claimed in claim 1 , comprising claim 1 , at the end of the reactive milling step claim 1 , a step of fluorination by bringing into contact with a fluorinating agent.5. The process as claimed in claim 1 , wherein the elements M and M′ are chosen from chromium claim 1 , nickel claim 1 , magnesium claim 1 , cobalt claim 1 , zinc claim 1 , aluminum claim 1 , antimony claim 1 , barium claim 1 , bismuth claim 1 , cadmium claim 1 , calcium claim 1 , cerium claim 1 , copper claim 1 , tin claim 1 , europium claim 1 , iron claim 1 , gallium claim 1 , germanium claim 1 , indium claim 1 , lanthanum claim 1 , manganese claim 1 , molybdenum claim 1 , nickel claim 1 , niobium claim 1 , phosphorus claim 1 , lead claim 1 , praseodymium claim 1 , scandium claim 1 , strontium claim 1 , tantalum claim 1 , terbium claim 1 , thorium claim 1 , titanium claim 1 , tungsten claim 1 , vanadium claim 1 , yttrium and zirconium.6. The ...

METHOD FOR SYNTHESIS OF LACTIC ACID AND ITS DERIVATIVES AND CATALYST FOR PREPARING SAME

The present disclosure provides a catalyst for preparing lactic acid and derivatives thereof, comprising at least one of metallic compounds MX, wherein M is selected from Na, K, Mg, Ca, Sr, Ba, Al, Ga, In, Sn, Sb, Bi, Cr, Mn, Fe, Co, Ni and Zn, and n is an integer of 1 to 6. The present disclosure further provides a method for synthesis of lactic acid and derivatives thereof, wherein at least one raw material including carbohydrates, at least one alcohol, at least one of the aforesaid catalysts and at least one solvent are heated to react to prepare lactic acid and derivatives thereof.

Electrochemical hydroxide systems and methods using metal oxidation

There are provided methods and systems for an electrochemical cell including an anode and a cathode where the anode is contacted with a metal ion that converts the metal ion from a lower oxidation state to a higher oxidation state. The metal ion in the higher oxidation state is reacted with hydrogen gas, an unsaturated hydrocarbon, and/or a saturated hydrocarbon to form products.

Process for Producing Chlorinated Hydrocarbons in the Presence of a Polyvalent Molybdenum Compound

The preparation of chlorinated hydrocarbons by reacting a chlorinated alkane substrate, such as 1,1,1,3-tetrachloropropane, with a source of chlorine, such as chlorine (Cl), in the presence of a polyvalent molybdenum compound, such as molybdenum pentachloride, is described. With the method of the present invention, the chlorinated alkane product has covalently bonded thereto at least one more chlorine group than the chlorinated alkane substrate, and the chlorinated alkane substrate and the chlorinated alkane product each have a carbon backbone structure that is in each case the same. 1. A method of preparing a chlorinated alkane product comprising ,reacting a chlorinated alkane substrate with a source of chlorine in the presence a polyvalent molybdenum compound, thereby forming a product comprising said chlorinated alkane product,wherein said chlorinated alkane product has covalently bonded thereto at least one more chlorine group than said chlorinated alkane substrate, andsaid chlorinated alkane substrate and said chlorinated alkane product each have a carbon backbone structure that is in each case the same.2. The method of claim 1 , wherein said source of chlorine is selected from chlorine (Cl) claim 1 , sulfuryl chloride claim 1 , and combinations thereof.3. The method of claim 1 , wherein said polyvalent molybdenum compound is selected from the group consisting of a tetravalent molybdenum compound claim 1 , pentavalent molybdenum compound claim 1 , a hexavalent molybdenum compound claim 1 , and combinations thereof.4. The method of claim 3 , wherein said tetravalent molybdenum compound comprises one or more tetravalent molybdenum compounds represented by the following Formula (I) claim 3 ,{'br': None, 'sup': '1', 'sub': a', 'b, 'Mo(R)(Cl)\u2003\u2003(I)'}wherein the sum of a and b is 2, 3, or 4, provided that b is 0, 1, 2, 3, or 4; and{'sup': '1', 'Rindependently for each a is oxygen.'}5. The method of claim 3 , wherein said tetravalent molybdenum compound is ...

CATALYTIC CHLORINATION OF 3,3,3-TRIFLUOROPROPENE TO 2,3-DICHLORO-1,1,1-TRIFLUOROPROPANE

The present invention relates to a process for preparing 1,1,1-trifluoro-2,3-dichloropropane which comprises contacting chlorine with 3,3,3-trifluoropropene in the presence of a catalyst to form 1,1,1-trifluoro-2,3-dichloropropane, wherein the catalyst comprises at least one metal halide, where the metal is a metal from Group 13, 14 or 15 of the periodic table or a transition metal or combination thereof. 1. A process for preparing 1 ,1 ,1-trifluoro-2 ,3-dichloropropane which comprises contacting chlorine with 3 ,3 ,3-trifluoropropene in the presence of a catalyst to form 1 ,1 ,1-trifluoro-2 ,3-dichloropropane , wherein the catalyst comprises at least one metal halide , where the metal is a metal from Group 13 , 14 or 15 of the periodic table or a transition metal or combination thereof.2. The process according to where at least one metal halide is supported on activated carbon which may optionally be acid washed or caustic washed.3. (canceled)4. The process according to wherein the metal is nickel claim 1 , chromium claim 1 , iron claim 1 , scandium claim 1 , yttrium claim 1 , lanthanum claim 1 , titanium claim 1 , zirconium claim 1 , hafnium claim 1 , vanadium claim 1 , molybdenum claim 1 , tungsten claim 1 , manganese claim 1 , rhenium claim 1 , ruthenium claim 1 , osmium claim 1 , cobalt claim 1 , palladium claim 1 , copper claim 1 , zinc claim 1 , tantalum claim 1 , aluminum claim 1 , tin claim 1 , or lead.5. The process according to wherein the metal halide is nickel halide claim 1 , iron halide or chromium halide.6. The process according to wherein the halide is a chloride.7. The process according to wherein the metal halide is nickel chloride claim 1 , iron halide or chromium halide.8. The process according to wherein the chlorination occurs in the vapor phase at a temperature ranging from about 80° C. to about 200° C. and a pressure ranging from about 10 psig to about 100 psig claim 1 , with the mole ratio of 3 claim 1 ,3 claim 1 ,3-trifluoropropene to ...

SELECTIVE CATALYTIC DEHYDROCHLORINATION OF HYDROCHLOROFLUOROCARBONS

A dehydrochlorination process is disclosed. The process involves contacting RCHClCHCl with a chromium oxyfluoride catalyst in a reaction zone to produce a product mixture comprising RCCl═CH, wherein Ris a perfluorinated alkyl group. 1. A composition comprising RCHClCHCl and a dehydrochlorination catalyst having the formula CrOF , wherein x+y/2=3 , wherein Ris a perfluorination alkyl group.2. The composition according to wherein Ris CFor CFCF.3. The composition according to wherein HF is additionally present.4. The composition according to wherein the mole ratio of HF to RCHClCHCl ranges from about 0.1:1 to about 50:1.5. The composition according to wherein the mole ratio HF to RCHClCHCl ranges from about 5:1 to about 25:1.6. The composition according to wherein the mole ratio HF to RCHClCHCl is no more than 0.9.7. The composition according to wherein the mole ratio HF to RCHClCHCl is no more than 0.5.8. The composition according to wherein the mole ratio HF to RCHClCHCl is no more than 0.1.9. The composition according to wherein an inert gas is additionally present.10. The composition according to wherein an inert gas is additionally present.11. The composition according to wherein RCCl═CHis additionally present.12. The composition according to wherein RCH═CHCl is additionally present.13. The composition according to wherein Ris CFor CFCF.14. The composition according to wherein Ris CFor CFCF.15. A composition comprising RCCl═CHand a dehydrochlorination catalyst having the formula CrOF claim 11 , wherein x+y/2=3 claim 11 , wherein Ris a perfluorination alkyl group.16. The composition according to wherein Ris CFor CFCF.17. A composition comprising 2-chloro-3 claim 15 ,3 claim 15 ,3-trifluoropropene ranging from 78 mol % to 95 mol %; 2 claim 15 ,3 claim 15 ,3 claim 15 ,3-tetrafluoropropene ranging from 0.6 mol % to 7.3 mol %; and 1-chloro-3 claim 15 ,3 claim 15 ,3-trifluoropropene ranging from 0.9 mol % to 4.2 mol %.18. The composition according to wherein 2-chloro-3 ...

Hydration catalyst, its preparation and application

FIELD: hydration catalysts. SUBSTANCE: invention relates to methods for preparing catalysts and their use. Described is a method for producing a hydrogenation catalyst, which includes the steps of: (1) contacting a first active metal component and a first organic complexing agent with a carrier to obtain a composite carrier; (2) calcining the composite carrier to obtain a calcined composite carrier in which the total carbon content, based on dry calcined composite carrier, is 1 wt% or less, and (3) contacting the second organic complexing agent with the calcined composite carrier to form a catalyst hydrogenation, wherein the process lacks any calcining step or any step for introducing a metal element active in the hydrogenation reaction during or after step (3). Described are methods of hydrotreating in the presence of a catalyst obtained and a composition containing the obtained catalyst I and a hydrogenation catalyst II other than catalyst I, the catalyst I being present in a volumetric amount from 5 to 95% with respect to the total volume of the catalyst composition. EFFECT: increased catalyst activity. 17 cl, 17 tbl, 96 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 37/02 B01J 37/08 B01J 27/02 B01J 21/00 C10G 45/00 (11) (13) 2 745 607 C2 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 37/02 (2021.02); B01J 37/08 (2021.02); B01J 27/02 (2021.02); B01J 21/00 (2021.02); C10G 45/00 (2021.02) (21)(22) Заявка: 2019106451, 24.04.2017 24.04.2017 Дата регистрации: 29.03.2021 12.09.2016 CN 201610817658.0; 12.09.2016 CN 201610818804.1; 12.09.2016 CN 201610819780.1 (43) Дата публикации заявки: 12.10.2020 Бюл. № 29 (56) Список документов, цитированных в отчете о поиске: CN 103551162 A, 05.02.2014. WO 2012133316 A1, 04.10.2012. WO 2012133319 A1, 04.10.2012. WO 2013093228 A1, 27.06.2013. RU 2249601 C2, 10.04.2005. (85) Дата начала рассмотрения заявки PCT на национальной фазе: ...

Methods for making supported chromium catalysts with increased polymerization activity

Methods for making a supported chromium catalyst are disclosed, and can comprise contacting a silica-coated alumina containing at least 30 wt. % silica with a chromium-containing compound in a liquid, drying, and calcining in an oxidizing atmosphere at a peak temperature of at least 650 °C to form the supported chromium catalyst. The supported chromium catalyst can contain from 0.01 to 20 wt. % chromium, and typically can have a pore volume from 0.5 to 2 mL/g and a BET surface area from 275 to 550 m 2 /g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

Methods for making supported chromium catalysts with increased polymerization activity

Methods for making a supported chromium catalyst are disclosed, and can comprise contacting a silica-coated alumina containing at least 30 wt. % silica with a chromium-containing compound in a liquid, drying, and calcining in an oxidizing atmosphere at a peak temperature of at least 650° C. to form the supported chromium catalyst. The supported chromium catalyst can contain from 0.01 to 20 wt. % chromium, and typically can have a pore volume from 0.5 to 2 mL/g and a BET surface area from 275 to 550 m 2 /g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

Methods for making fluorided chromium (VI) catalysts, and polymerization processes using the same

Methods for preparing a fluorided chromium catalyst can include a step of calcining a supported chromium catalyst at a peak calcining temperature to produce a calcined supported chromium catalyst, followed by contacting the calcined supported chromium catalyst at a peak fluoriding temperature with a vapor comprising a fluorine-containing compound to produce the fluorided chromium catalyst. The peak fluoriding temperature can be at least 50° C. less, and often from 200° C. to 500° C. less, than the peak calcining temperature. Polymers produced using the fluorided chromium catalyst can have a beneficial combination of higher melt index, narrower molecular weight distribution, and lower long chain branch content.

Methods for making fluorided chromium (vi) catalysts, and polymerization processes using the same

Methods for preparing a fluorided chromium catalyst can include a step of calcining a supported chromium catalyst at a peak calcining temperature to produce a calcined supported chromium catalyst, followed by contacting the calcined supported chromium catalyst at a peak fluoriding temperature with a vapor comprising a fluorine-containing compound to produce the fluorided chromium catalyst. The peak fluoriding temperature can be at least 50 oC less, and often from 200 oC to 500 oC less, than the peak calcining temperature. Polymers produced using the fluorided chromium catalyst can have a beneficial combination of higher melt index, narrower molecular weight distribution, and lower long chain branch content.

Ionic liquid catalyst having enhanced activity

A process for producing acidic ionic liquid catalyst having enhanced activity comprising combining fresh acidic ionic liquid catalyst, a metal and a Broensted acid in a reaction zone for a time sufficient to increase the activity of the ionic liquid catalyst is disclosed. A process for producing acidic ionic liquid catalyst having enhanced activity comprising the steps of combining fresh ionic liquid catalyst, a metal and HCl in a reaction zone for a time sufficient to increase the activity of the fresh ionic liquid catalyst; removing reaction product from the reaction zone and recovering at least a portion of the treated ionic liquid catalyst is also disclosed.

A hydrogenation catalyst and use thereof

A hydrogenation catalyst comprises a support, metal active components consisting of Ni, Mo and W which are carried on the support, and auxiliary active components selected from the group consisting of F , P or their combination. Another hydrogenation catalyst comprises a support having molecular sieve component, metal active components consisting of Ni, Mo and W which are carried on the support . The catalysts can be used in methods for hydrogenation of hydrocarbon oil .The catalysts have higher catalytic activity than conventional catalysts.

Process for preparing fluorination catalyst

A process for preparing a fluorination catalyst using a low pressure activating step followed by a high pressure activating step.

Processo para preparar pentafluoroetano

Processo para produzir um composto

Catalyst and process using the catalyst

Catalyst and process using the catalyst

Catalyst and processes for olefin trimerization

A process is provided to modify an olefin production catalyst system which comprises contacting an olefin production catalyst system with ethylene prior to use. A second embodiment of the invention comprises contacting an aluminum alkyl and a pyrrole-containing compound prior to contacting a chromium containing compound and prior to contacting an olefin. A process also is provided to trimerize and/or oligomerize olefins with the novel, modified olefin catalyst production systems. These modified olefin production catalyst systems can produce less solids, such as, for example, polymer, during a trimerization reaction.

Catalyst and processes for olefin trimerization

methods for producing supported chromium catalysts with increased polymerization activity

MÉTODOS PARA PRODUZIR CATALISADORES DE CROMO SUPORTADOS COM ATIVIDADE DE POLIMERIZAÇÃO AUMENTADA. Métodos para produzir um catalisador de cromo suportado são divulgados e podem compreender colocar uma alumina revestida com sílica contendo pelo menos 30% em peso de sílica em contato com um composto contendo cromo em um líquido, secar e calcinar em uma atmosfera oxidante a uma temperatura de pico de pelo menos 650°C para formar o catalisador de cromo suportado. O catalisador de cromo suportado pode conter de 0,01 a 20% em peso de cromo e, normalmente, pode ter um volume de poro de 0,5 a 2 ml/g e uma área de superfície BET de 275 a 550 m²/g. O catalisador de cromo suportado subsequentemente pode ser usado para polimerizar olefinas para produzir, por exemplo, homopolímeros e copolímeros à base de etileno tendo pesos moleculares elevados e distribuições de peso molecular amplas. METHODS TO PRODUCE CHROME CATALYST SUPPORTED WITH INCREASED POLYMERIZATION ACTIVITY. Methods for producing a supported chromium catalyst are disclosed and may comprise placing a silica coated alumina containing at least 30% by weight silica in contact with a chromium containing compound in a liquid, drying and calcining in an oxidizing atmosphere at a temperature of peak of at least 650°C to form the supported chromium catalyst. The supported chromium catalyst may contain from 0.01 to 20% by weight of chromium and typically may have a pore volume of 0.5 to 2 ml/g and a BET surface area of 275 to 550 m²/g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

Hydrogenation catalyst, its production and application thereof

The present application relates to a hydrogenation catalyst, a process for producing the same and application thereof in the hydrotreatment of feedstock oil. The process comprises at least the following steps: (1) contacting a first active metal component and a first organic complexing agent with a carrier to obtain a composite carrier; (2) calcining the composite carrier to obtain a calcined composite carrier having a total carbon content of 1% by weight or less; and (3) contacting a second organic complexing agent with the calcined composite carrier to obtain the hydrogenation catalyst. The hydrogenation catalyst has both excellent hydrodesulfurization activity and hydrodenitrogenation activity, and exhibits a significantly prolonged service life.

Катализатор гидрирования, его получение и применение

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 37/02 B01J 37/08 B01J 27/02 B01J 21/00 C10G 45/00 (11) (13) 2019 106 451 A (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2019106451, 24.04.2017 (71) Заявитель(и): ЧАЙНА ПЕТРОЛЕУМ ЭНД КЕМИКАЛ КОРПОРЕЙШЕН (CN), РИСЕРЧ ИНСТИТУТ ОФ ПЕТРОЛЕУМ ПРОЦЕССИНГ, СИНОПЕК (CN) Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 12.10.2020 Бюл. № 29 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 12.04.2019 CN 2017/000318 (24.04.2017) (87) Публикация заявки PCT: A WO 2018/045693 (15.03.2018) Адрес для переписки: 119019, Москва, Гоголевский бульвар,11, Гизатуллина Евгения Михайловна R U (57) Формула изобретения 1. Способ получения катализатора гидрирования, предусматривающий стадии, на которых: (1) вводят в контакт первый активный металлический компонент, первый органический комплексообразующий агент и необязательный соагент с носителем и получают композиционный носитель; (2) прокаливают композиционный носитель и получают прокаленный композиционный носитель, в котором полное содержание углерода в расчете на сухой прокаленный композиционный носитель составляет 1 мас.% или менее, 0,5 мас.% или менее, 0,4 мас.% или менее, 0,3 мас.% или менее, 0,1 мас.% или менее, 0,08 мас.% или менее, 0,06 мас.% или менее, 0,04 мас.% или менее, 0,03 мас.% или менее, 0,01 мас.% или менее, или 0,005 мас.% или менее по отношению к сухой массе прокаленного композиционного носителя; и (3) вводят в контакт второй органический комплексообразующий агент с прокаленным композиционным носителем и получают катализатор гидрирования, и необязательно способ дополнительно предусматривает одну или несколько из стадий, на которых: (0) получают носитель; и (4) сульфурируют катализатор гидрирования. Стр.: 1 A 2 0 1 9 1 0 6 4 5 1 (54) КАТАЛИЗАТОР ГИДРИРОВАНИЯ, ЕГО ПОЛУЧЕНИЕ И ПРИМЕНЕНИЕ 2 0 1 9 1 0 6 4 5 1 (86) Заявка PCT: (72) Автор(ы): ЧЖАН, ...

一种加氢催化剂组合物和加氢处理的方法

本公开涉及一种加氢催化剂组合物和加氢处理的方法，该加氢催化剂组合物包括加氢催化剂I和加氢催化剂II；以体积计并以所述加氢催化剂组合物为基准，所述加氢催化剂I的含量为5‑95％；所述加氢催化剂I包括载体、加氢活性金属元素和金属助剂元素，所述加氢活性金属元素含有第VIB族金属元素和第VIII族金属元素；其中，所述加氢催化剂I的制备方法包括：将负载有含加氢活性金属元素的化合物、第一有机络合剂和金属助剂元素的载体进行第一干燥和焙烧，得到半成品催化剂；将第二有机络合剂负载到所述半成品催化剂上，并进行第二干燥且不进行焙烧，得到所述加氢催化剂I。将本公开提供的加氢催化剂组合物应用于加氢处理时，活性好，寿命长。

一种加氢催化剂组合物和加氢处理的方法

本公开涉及一种加氢催化剂组合物和加氢处理的方法，该加氢催化剂组合物包括加氢催化剂I和加氢催化剂II；以体积计并以所述加氢催化剂组合物为基准，所述加氢催化剂I的含量为5‑95％；所述加氢催化剂I包括载体、加氢活性金属元素和非金属助剂元素，所述加氢活性金属元素含有第VIB族金属元素和第VIII族金属元素；其中，所述加氢催化剂I的制备方法包括：将负载有含加氢活性金属元素的化合物、第一有机络合剂和非金属助剂元素的所述载体进行第一干燥和焙烧，得到半成品催化剂；将第二有机络合剂负载到所述半成品催化剂上，并进行第二干燥且不进行焙烧，得到所述加氢催化剂I。将本公开提供的加氢催化剂组合物应用于加氢处理时，活性好，寿命长。

一种加氢催化剂组合物和加氢处理的方法

本发明涉及一种加氢催化剂组合物和加氢处理的方法，该加氢催化剂组合物包括加氢催化剂I和加氢催化剂II；以体积计并以所述加氢催化剂组合物为基准，所述加氢催化剂I的含量为5‑95％，所述加氢催化剂II的含量为5‑95％；其中，所述加氢催化剂I的制备方法包括：(1)将加氢活性金属组分和有机络合剂负载到载体上，并进行第一干燥并焙烧，得到催化剂前体；(2)将有机络合剂负载到所述催化剂前体上，并进行第二干燥，得到所述加氢催化剂I。将本发明提供的加氢催化剂组合物应用于加氢处理时，活性好，寿命长。

Hydrogenation catalyst, manufacturing method therefor, and application thereof

A hydrogenation catalyst and a manufacturing method therefor. The manufacturing method at least comprises: (1) contacting a first active metal component and a first organic complexing agent with a carrier to obtain a composite carrier; (2) calcining the composite carrier to obtain a calcined composite carrier, the total content of carbon in the calcined composite carrier being less than 1 wt%; and (3) contacting a second organic complexing agent with the calcined composite carrier to obtain a hydrogenation catalyst. The hydrogenation catalyst has excellent hydrogenation desulfurization activity and hydrogenation denitrification activity, and shows significantly extended catalyst service life.

Hydrogenation catalyst, manufacturing method therefor, and application thereof

Hydrogenation catalysts, their manufacture and their applications

Hydrogenation catalyst, its production and application thereof

The present application relates to a hydrogenation catalyst, a process for producing the same and application thereof in the hydrotreatment of feedstock oil. The process comprises at least the following steps: (1) contacting a first active metal component and a first organic complexing agent with a carrier to obtain a composite carrier; (2) calcining the composite carrier to obtain a calcined composite carrier having a total carbon content of 1% by weight or less; and (3) contacting a second organic complexing agent with the calcined composite carrier to obtain the hydrogenation catalyst. The hydrogenation catalyst has both excellent hydrodesulfurization activity and hydrodenitrogenation activity, and exhibits a significantly prolonged service life. No Figure

A hydrogenation catalyst and its application

Hydrogenation catalyst, manufacturing method therefor, and application thereof

The present application relates to a hydrogenation catalyst, a process for producing the same and application thereof in the hydrotreatment of feedstock oil. The process comprises at least the following steps: (1) contacting a first active metal component and a first organic complexing agent with a carrier to obtain a composite carrier; (2) calcining the composite carrier to obtain a calcined composite carrier having a total carbon content of 1% by weight or less; and (3) contacting a second organic complexing agent with the calcined composite carrier to obtain the hydrogenation catalyst. The hydrogenation catalyst has both excellent hydrodesulfurization activity and hydrodenitrogenation activity, and exhibits a significantly prolonged service life.

Catalyst and processes for olefin trimerization

A process is provided to modify an olefin production catalyst system which comprises contacting an olefin production catalyst system with ethylene prior to use. A second embodiment of the invention comprises contacting an aluminium alkyl and a pyrrole-containing compound prior to contacting a chromium containing compound and prior to contacting an olefin. A process also is provided to trimerize and/or oligomerize olefins with the novel, modified olefin catalyst production systems. These modified olefin production catalyst systems can produce less solids, such as, for example, polymer, during a trimerization reaction.

Fluorination catalysts, method for their preparation, and method for producing fluorinated compounds using the catalysts

The present invention provides a novel fluorination catalyst that has high stability at high temperatures, is easily regenerated and is superior in catalytic activity and selectivity and a method for the preparation of the fluorination catalyst. The present invention also provides a method for the preparation of a novel fluorinated compound, and particularly, 1,1,1,3,3-pentafluoropropane (HFC-245fa), by using the catalyst. The fluorination catalyst of the present invention is obtained by treating a metal salt containing a chromium salt such as chromium oxide with chlorine gas and/or oxygen gas. Examples of the metal salt may include, besides a chromium salt, one or more catalytically active metal salts selected from magnesium salts, aluminum salts, zinc salts, sodium salts, nickel salts, iron salts, cobalt salts, vanadium salts, manganese salts and copper salts.

Methods for making supported chromium catalysts with increased polymerization activity

Methods for making a supported chromium catalyst are disclosed, and can comprise contacting a silica-coated alumina containing at least 30 wt. % silica with a chromium-containing compound in a liquid, drying, and calcining in an oxidizing atmosphere at a peak temperature of at least 650 °C to form the supported chromium catalyst. The supported chromium catalyst can contain from 0.01 to 20 wt. % chromium, and typically can have a pore volume from 0.5 to 2 mL/g and a BET surface area from 275 to 550 m2/g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

Fluorination catalyst and fluorination process

一种1,1-二氟乙烯的制备方法

本发明公开了一种1,1‑二氟乙烯的制备方法，包括以下步骤：复合型催化剂装填入管式反应器中，以1,1‑二氟‑1‑氯乙烷或1,1‑二氟‑2‑氯乙烷为原料通入所述管式反应器中，进行气相催化裂解反应，制得1,1‑二氟乙烯；所述复合型催化剂为所述复合型催化剂为金属复合氟化物。本发明提供的制备1,1‑二氟乙烯的方法具有反应温度低，产物选择性高、收率高、催化剂可再生性强、制备工艺条件温和、操作简单等特点。

Method of preparing 1,1,1,2-tetrafluoroethane, pentafluoroethane and 1,1,1-trifluoroethane

불화칼슘과, 삼산화크롬, 염화아연 및 염화제2철의 수용액을 혼합한후 에탄올과 반응시켜 얻어지는 생성물을 소성함으로써 제조된 촉매의 존재하에, 1단계 반응으로서, 1,1,1-트리플루오로-2-클로로에탄(HCFC-133a)과 불화수소를 반응시켜 1,1,1,2-테트라플루오로에탄(HFC-134a), 펜타플루오로에탄(HFC-125) 및 1,1,1,-트리플루오로에탄(HFC-143a)을 얻고, 2단계 반응으로서 1단계 반응생성물에 트리클로로에틸렌을 첨가하여 HCFC-133a를 제조한 다음 HFC-134a, HFC-125 및 HFC-143a를 분리하고 HCFC-133a를 1단계 반응으로 재순환시키는 것으로 이루어지는 2단계 기상반응에 의해, HFC-134a, HFC-125 및 HFC-143a를 동시에 제조하는 방법이 제공된다. 1,1,1-trifluoro as a one-step reaction in the presence of a catalyst prepared by mixing calcium fluoride with an aqueous solution of chromium trioxide, zinc chloride and ferric chloride, and then calcining the product obtained by reacting with ethanol. 2-chloroethane (HCFC-133a) and hydrogen fluoride were reacted to give 1,1,1,2-tetrafluoroethane (HFC-134a), pentafluoroethane (HFC-125) and 1,1,1, -Trifluoroethane (HFC-143a) was obtained, HCFC-133a was prepared by adding trichloroethylene to the first stage reaction product as a two-step reaction, and then HFC-134a, HFC-125 and HFC-143a were separated and HCFC By a two-stage gas phase reaction consisting of recycling -133a to a one-stage reaction, a method for simultaneously producing HFC-134a, HFC-125 and HFC-143a is provided.

一种溴化氧铋/钼酸铋异质结光催化剂及制备与应用

本发明属于光催化材料技术领域，公开了一种溴化氧铋/钼酸铋异质结光催化剂及制备与应用。所述方法为：(1)溶剂热法制备Bi 2 MoO 6 微球；(2)将Bi 2 MoO 6 微球在水中分散成Bi 2 MoO 6 水分散液，将Bi(NO 3 ) 3 乙二醇溶液缓慢加入Bi 2 MoO 6 水分散液中，搅拌均匀，得到混合分散液；(3)将十六烷基三甲基溴化铵乙二醇溶液缓慢加入混合分散液中，在室温条件下进行搅拌反应，在高温下进行无搅拌反应，洗涤，干燥，得到溴化氧铋/钼酸铋异质结光催化剂。所述光催化剂光催化活性高，稳定性良好；制备方法简单，易于批量生产；用于有机污染物如罗丹明B等物质的光催化降解。

一种hfc-23资源化利用中提高催化剂稳定性的方法

本发明公开了一种HFC‑23资源化利用中提高催化剂稳定性的方法，所述资源化利用采用HFC‑23和卤代烃进行氟氯交换反应实现，所述氟氯交换反应的催化剂包括主体催化剂和金属氧化物，所述金属氧化物选自K、Na、Fe、Co、Cu、Ni、Zn或Ti中的至少一种金属氧化物，添加量为0.1～5wt％。本发明具有催化剂稳定性好、寿命长，副产CFC‑12含量低等优点。

1, 1, 1, 2-테트라플루오로에탄의 제조방법

내용 없음.

Catalysts and methods of using the catalysts to prepare fluorinated hydrocarbons

크로미아 및 하나 이상의 금속 산화물을 포함하는 촉매로서, 상기 촉매는 0.3cm 3 /g 이상의 총 기공 부피를 가지며 평균 기공 직경은 90Å 이상이며, 상기 기공 부피는 N 2 흡착 기공측정법을 사용하여 측정되며, 상기 평균 기공 직경은 N 2 BET 흡착 기공측정법을 사용하여 측정된다. A catalyst comprising chromia and one or more metal oxides, wherein the catalyst has a total pore volume of at least 0.3 cm 3 /g and an average pore diameter of at least 90 Å, wherein the pore volume is determined using N 2 adsorption porosimetry, The average pore diameter is measured using N 2 BET adsorption porosimetry.

氟化催化剂及其制备方法、以及使用了该催化剂的氟化合物的制备方法

本发明的氟化催化剂是，通过对含有氧化铬等铬盐的金属盐用氯气/或氧气进行处理而得到的。作为金属盐，除了铬盐以外，可以举出具有催化活性的从镁、铝、锌、钠、镍、铁、钴、钒、锰、铜中选择一种以上元素的金属盐。通过本发明可以提供高温下的稳定性高、再生容易且具有出色的催化活性或选择性的新的氟化催化剂和其制备方法，另外还可以提供使用了这些催化剂的新的氟化合物制备方法，尤其1，1，1，3，3—五氟丙烷(HFC-245fa)的制备方法。

气相氟化制备e-1,1,1,4,4,4-六氟-2-丁烯的方法

本发明公开了一种气相氟化制备E‑1,1,1,4,4,4‑六氟‑2‑丁烯的方法，即：在氟化催化剂存在下，四氟丁三烯或者四氯丁三烯，与氟化氢发生氟化反应，得到E‑1,1,1,4,4,4‑六氟‑2‑丁烯。本发明主要用于高效率、连续循环地生产E‑1,1,1,4,4,4‑六氟‑2‑丁烯。

Methods for Making Supported Chromium Catalysts with Increased Polymerization Activity

Methods for making a supported chromium catalyst are disclosed, and can comprise contacting a silica-coated alumina containing at least 30 wt. % silica with a chromium-containing compound in a liquid, drying, and calcining in an oxidizing atmosphere at a peak temperature of at least 650° C. to form the supported chromium catalyst. The supported chromium catalyst can contain from 0.01 to 20 wt. % chromium, and typically can have a pore volume from 0.5 to 2 mL/g and a BET surface area from 275 to 550 m2/g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

증가된 중합 활성을 갖는 지지된 크롬 촉매를 제조하는 방법

본원은 지지된 크롬 촉매를 제조하는 방법을 개시하며, 이는 적어도 30 중량%의 실리카를 함유하는 실리카-코팅된 알루미나를 크롬-함유 화합물과 액체 중에서 접촉시키고, 건조시키고, 적어도 650℃의 피크 온도에서 산화 분위기에서 하소하여 상기 지지된 크롬 촉매를 형성하는 단계를 포함할 수 있다. 상기 지지된 크롬 촉매는 0.01 내지 20 중량%의 크롬을 함유할 수 있으며, 전형적으로, 0.5 내지 2 mL/g의 기공 부피 및 275 내지 550 m 2 /g의 BET 표면적을 가질 수 있다. 이어서, 상기 지지된 크롬 촉매는, 예를 들어, 고분자량 및 넓은 분자량 분포를 갖는 에틸렌계 단독 중합체 및 공중합체를 제조하기 위해 올레핀을 중합하는 데 사용될 수 있다.

制备具有增强的聚合活性的负载型铬催化剂的方法

公开了用于制备负载型铬催化剂的方法，所述方法可包括使含有至少30重量％的二氧化硅的二氧化硅涂覆的氧化铝与含铬化合物在液体中接触，干燥，并在氧化气氛中在至少650℃的峰值温度下煅烧以形成所述负载型铬催化剂。所述负载型铬催化剂可含有0.01重量％至20重量％的铬，并且通常可具有0.5mL/g至2mL/g的孔隙体积和275m 2 /g至550m 2 /g的BET表面积。随后可以使用负载型铬催化剂来使烯烃聚合，以产生例如具有高分子量和宽分子量分布的基于乙烯的均聚物和共聚物。

Methods for making supported chromium catalysts with increased polymerization activity

Methods for making a supported chromium catalyst are disclosed, and can comprise contacting a silica-coated alumina containing at least 30 wt. % silica with a chromium-containing compound in a liquid, drying, and calcining in an oxidizing atmosphere at a peak temperature of at least 650 °C to form the supported chromium catalyst. The supported chromium catalyst can contain from 0.01 to 20 wt. % chromium, and typically can have a pore volume from 0.5 to 2 mL/g and a BET surface area from 275 to 550 m 2 /g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

氟化催化剂的制备方法

一种使用低压活化步骤接着高压活化步骤制备氟化催化剂的方法。

含卤素水合氧化铝组合物和成型体及制备方法以及催化剂及其制备方法

本发明公开了一种含卤素水合氧化铝组合物及其制备方法以及成型体及其制备方法和应用，该组合物含有水合氧化铝、含卤素化合物和具有至少两个质子受体位点的化合物，该组合物的 值为不低于1.8。本发明还公开了以由所述含卤素水合氧化铝组合物形成的成型体作为载体的具有加氢催化作用的催化剂及制备方法和加氢处理方法。本发明以水合氧化铝湿凝胶为起始原料制备得到具有较高强度的成型体，省略了用于干燥水合氧化铝湿凝胶的步骤，简化了总体工艺流程，降低了总体操作能耗，避免了由于采用拟薄水铝石干胶粉作为原料而引发的粉尘污染。由该水合氧化物组合物形成的成型体作为载体制备的催化剂在烃油的加氢处理中显出更高的催化活性。

Catalysts and methods of using the catalysts to prepare fluorinated hydrocarbons

크로미아 및 적어도 하나의 추가의 금속 또는 이의 화합물을 포함하는 촉매로서, 상기 촉매는 0.3 cm 3 /g을 초과하는 총 기공 부피를 가지며 평균 기공 직경은 90Å 이상이며, 상기 총 기공 부피는 N2 흡착 기공측정법에 의해 측정되며, 상기 평균 기공 직경은 N 2 BET 흡착 기공측정법에 의해 측정되며, 상기 적어도 하나의 추가의 금속은 Li, Na, K, Ca, Mg, Cs, Sc, Al, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Re, Fe, Ru, Co, Rh, Ir, Ni, Pd, In, Pt, Cu, Ag, Au, Zn, La, Ce 및 이들의 혼합물로부터 선택된다. A catalyst comprising chromia and at least one additional metal or compound thereof, wherein the catalyst has a total pore volume greater than 0.3 cm 3 /g and an average pore diameter of at least 90 Å, wherein the total pore volume comprises N2 adsorption pores and wherein the mean pore diameter is determined by N 2 BET adsorption porosimetry, wherein the at least one additional metal is Li, Na, K, Ca, Mg, Cs, Sc, Al, Y, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, Re, Fe, Ru, Co, Rh, Ir, Ni, Pd, In, Pt, Cu, Ag, Au, Zn, La, Ce and selected from mixtures thereof.

生产并纯化含氯氟烃和氟化烃的物质与方法

提供基本上异构纯的全卤化和部分卤化化合物的方法与物质。本发明的一个实施方案提供生产基本上异构纯CFC－216aa的方法。其它实施方案包括生产CFC－217ba和HFC－227ea的方法。本发明特别的实施方案提供从HF、从其它含氯氟烃中分离含氯氟烃和分离卤化化合物的异构体的分离技术。本发明又一其它的实施方案提供具有延长的催化剂寿命的催化合成技术。在其它实施方案中，本发明提供纯化异构体混合物的催化技术。

1,1,1,2-테트라플루오로-2-클로로에탄 및 펜타플루오로에탄의 제조방법

본 발명은 1,1,1,2-테트라플루오로-2-클로로에탄 및 펜타플루오르에탄의 제조방법에 관한 것이다. 식 C 2 HX 2-1 F 3+1 (식중, X는 염소 또는 브롬원자이고, n은 0또는 1)의 펜타할로에탄 하나 이상을 불화수소산을 사용하여 기상 촉매 불화시키는 것으로 이루어진 방법은 불화 알루미늄 또는 불화 알루미늄과 알루미나의 혼합물로 구성된 지지체 상에 침착된 니켈 및 크롬의 산화물, 할로겐화물 및/또는 옥시 할로겐화물로 이루어진 혼합 촉매를 사용함을 특징으로 한다.

Method of producing fluorization catalyst for preparing 1,1,1,2-tetrafluoroethane

A mixture of chrom oxide hydride and magnesium or calcium chloride in the ratio of 1 : 0.3 and 1 : 10 is mixed in a metal salt solution, and reacted with hydrogen fluoride solution, followed by, curing the obtained paste mixture. The ratio of chrom and magnesium or calcium is between 1 : 1 and 1 : 4, and the metal salt is selected from cerium chloride, zinc chloride, nickel chloride and aluminium chloride.

Cerium chloride-chromium oxide catalyst for producing chlorine by oxidation of hydrochloric acid and method for manufacture thereof

The catalyst is manufactured by (a) adding ethanol to the mixture of CrO3, CeCl3 and water; (b) obtaining hydrated CeCl3-Cr2O3 by reflux reaction above 90 deg.C; (c) drying under 100-140 deg.C; (d) forming under 360-380 deg.C for 3-6 hrs. Another method is to (a) obtain Cr2O3 sediment from the reaction of CrO3 and ethanol; (b) dry and form; (c) add CeCl3. The catalyst shows better activity at lower temp. than established catalyst. For example, the conversion rate of hydrogen chloride is 75-85% at reaction temp. 360-380 deg.C. in case of using this catalyst.

Preparation method of olefin polymerization catalyst and preparation method of poly α -olefin base oil

本发明涉及一种烯烃聚合催化剂的制备方法，该催化剂为Cr‑AlCl 3 /Al 2 O 3 固载催化剂，该方法包括以下步骤：(1)将γ‑Al 2 O 3 载体加入到含铬盐的溶液中，在搅拌条件下，加入氨水反应，过滤、干燥后在惰性气体保护条件下，高温焙烧，得到Cr/γ‑Al 2 O 3 ；(2)将Cr/γ‑Al 2 O 3 加入三氯化铝甲苯溶液中，回流除去溶剂后，甲苯洗涤，真空干燥得到Cr‑AlCl 3 /Al 2 O 3 催化剂。本发明还涉及一种聚α‑烯烃基础油的制备方法，以上述方法制备的催化剂为烯烃聚合催化剂。本发明的催化剂催化α‑烯烃齐聚反应活性高，产物中氯含量较低，避免了均相催化剂对反应器的腐蚀。

Halogen promoted polymetallic oxide catalyst

包含促进的混合金属氧化物的催化剂,适用于链烷烃或链烷烃和链烯烃的混合物至不饱和羧酸的气相氧化,并适用于链烷烃或链烷烃和链烯烃的混合物至不饱和腈的气相氨氧化。

Process for the manufacture of 1,1,1,2-tetrafluoro-2-chloroethane and of pentafluoroethane

本发明涉及制备1，1，1，2-四氟-2-氯乙烷和五 氟乙烷的方法。本方法对至少一种五卤乙烷C 2 HX 2-n F 3+n 用氢氟酸进行气相催化氟化。其特征在于采用沉积在由氟化铝或氟化铝和氧化铝混合物构成的载体上的由镍和铬的氧化物、卤化物和/或氧卤化物组成的混合催化剂。

Process for the manufacture of halogenated propanes containing end-carbon fluorine

公开制备下式化合物的方法:CF 3 CHXCF 3－Z Y Z ,其中X和Y独立地选自H和Cl,z为0或1。所述方法包括(1)在低于200℃温度下,使CCl 3 CHXCC 3－Z Y Z 、CCl 2－Z Y Z =CXCC 3 和/或CCl 2 CX=CC 3－Z Y Z 原料与氟化氢接触产生所述原料的氟化产物,该产物包括至少90%(摩尔)的总的C 3 HXY Z Cl 6－Z－X F X 饱和的化合物和C 3 XY Z Cl 5－Z－Y F Y 烯属化合物,其中x为1至6－z的整数,y为1至5－z的整数(氟化产物包括不超过约40%(摩尔)的所需产物,CF 3 CHXCF 3－Z Y Z );(2)在氟化催化剂存在下,在温度200℃至约400℃温度范围内,使在(1)中产生的饱和化合物和烯属化合物于汽相中与氟化氢接触;(3)在汽相氟化催化剂的存在下,在温度200℃至约400℃温度范围内,使足够量的所述化合物,其中x为1至5－z的整数和在(1)中产生的烯属化合物于汽相中与氟化氢反应提供基于在(1)和(2)中与HF反应的原料量的至少约90%对CF 3 CHXCF 3－Z Y Z 的总的选择性。

Halogen Promoted Multi-Metal Oxide Catalyst

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

Fluorination catalyst and fluorination process

A fluorination catalyst comprising indium, chromium, oxygen and fluorine as essential constituent elements thereof. The catalyst is prepared by fluorinating a catalyst precursor comprising indium and chromium elements by bringing it into contact with hydrogen fluoride or a fluorine-containing halogenated hydrocarbon at a temperature of 300° to 500° C. A halogenated hydrocarbon is fluorinated by bringing it into contact with hydrogen fluoride in a gaseous phase in the presence of the catalyst.

Processes for purifying chlorofluorinated compounds and processes for purifying cf3cfhcf3

提供基本上异构纯的全卤化和部分卤化化合物的方法与物质。本发明的一个实施方案提供生产基本上异构纯CFC-216aa的方法。其它实施方案包括生产CFC-217ba和HFC-227ea的方法。本发明特别的实施方案提供从HF、从其它含氯氟烃中分离含氯氟烃和分离卤化化合物的异构体的分离技术。本发明又一其它的实施方案提供具有延长的催化剂寿命的催化合成技术。在其它实施方案中，本发明提供纯化异构体混合物的催化技术。

Ethylene trimerization using a supported chromium-tantalum catalyst

Bimetallic, supported catalysts for production of 1-hexene from ethylene are manufactured by impregnating a porous, solid support material with at least one catalytic chromium compound and at least one catalytic tantalum compound. The bimetallic, supported catalysts have high catalytic turnover, high selectivity for 1-hexene production, a low tendency for metals to leach from the catalysts during manufacturing and use compared to catalysts manufactured using known techniques. Moreover, the catalysts can be reused in multiple synthesis runs. High turnover, high selectivity, and reusability improve yields and reduce the costs associated with producing 1-hexene from ethylene, while the absence of metal leaching reduces the potential environmental impacts of using toxic metal catalysts (e.g., chromium).