КАТАЛИЗАТОР НА ОСНОВЕ СМЕШАННЫХ ОКСИДОВ ДЛЯ ГИДРИРОВАНИЯ ОРГАНИЧЕСКИХ СОЕДИНЕНИЙ, СПОСОБ ЕГО ПОЛУЧЕНИЯ И СПОСОБ ГИДРИРОВАНИЯ

Изобретение относится к катализатору на основе смешанных оксидов для гидрирования органических соединений, способу его получения и способу гидрирования. Описан катализатор для гидрирования органических соединений, получаемый восстановлением предварительного катализатора, состоящего из а) кобальта и b) одного или нескольких элементов группы щелочных металлов или щелочноземельных металлов, причем элементы а) и b) по меньшей мере частично находятся в виде их смешанных оксидов. Описан способ получения катализатора для гидрирования органических соединений путем восстановления указанного выше предварительного катализатора. Описан способ гидрирования соединений, содержащих по меньшей мере одну ненасыщенную углерод-углеродную, углерод-азотную или углерод-кислородную связь или частичного или полного гидрирования ядра ароматических соединений с использованием описанного выше катализатора. Технический эффект - повышение стабильности катализатора и упрощение технологии гидрирования органических соединений ...

Способ подготовки катализаторов гидрогенизационных процессов к окислительной регенерации

Изобретение относится к способу подготовки катализаторов гидроочистки к окислительной регенерации путем обработки пассивированного сульфидного катализатора, содержащего NiO, VO, FeO, смесью бутилцеллозольва и нефраса, в которой растворен комплексообразователь, выбранный из щавелевой, винной или лимонной кислоты. Также изобретение относится к способу регенерации раствора комплексообразователя, полученного после осуществления способа обработки пассивированного сульфидного катализатора. Технический результат заключается в увеличении каталитической активности. 2 н. и 6 з.п. ф-лы, 3 табл., 9 пр.

РЕГЕНЕРИРОВАННЫЙ КАТАЛИЗАТОР ГИДРООБРАБОТКИ

Изобретение относится к регенерированному катализатору гидрообработки, восстановленному из катализатора гидрообработки для очистки нефтяной фракции. При этом данный катализатор гидрообработки получен посредством закрепления молибдена и по меньшей мере одного компонента, выбранного из металлов групп 8-10 Периодической таблицы, на неорганическом носителе, содержащем оксид алюминия, в котором содержание остаточного углерода находится в интервале от 0,15 масс.% до 3,0 масс.%, интенсивность пика молибденсодержащего сложного оксида металлов по отношению к интенсивности основного пика находится в интервале от 0,60 до 1,10 в рентгеновском дифракционном спектре (Х-Ray), и либо интенсивность пика связи Mo-S, производной от пика остаточной серы, по отношению к интенсивности основного пика находится в интервале от 0,10 до 0,60 на кривой радиального распределения, полученной из спектра протяженной тонкой структуры рентгеновского поглощения при анализе тонкой структуры рентгеновского поглощения, либо ...

УСТРОЙСТВО ДЛЯ НАГРЕВАНИЯ СЫПУЧИХ МАТЕРИАЛОВ

Предлагается устройство для нагревания сыпучих материалов в гидрогенизационных процессах, включающее цилиндрический барабан, вращающийся вокруг оси со скоростью от 2 до 4 об/мин, с внутренним устройством для распределения сыпучего материала в потоке нагреваемого вне устройства рабочего газа и перемещения его в рабочей зоне барабана, при условии, что внутреннее устройство выполнено в виде системы чередующихся вдоль стенок барабана горизонтальных полок длиной, равной длине рабочей зоны барабана, и горизонтальных полок длиной, равной ее половине, с образованием между двумя соседними длинными полками щели для подачи рабочего газа с возможностью омывания им промежуточной полки, при этом устройство снабжено термопреобразователями для регулирования температуры в слое сыпучего материала, расположенными по ходу движения сыпучего материала, размер рабочей зоны барабана составляет от 8 м до 10 м длиной, предпочтительно 9 м, диаметром от 2,5 м до 2,9 м, предпочтительно 2,66 м, длина чередующихся горизонтальных ...

СПОСОБ ДЕГИДРИРОВАНИЯ ЭТИЛБЕНЗОЛА ДО СТИРОЛА

Использование: получение углеводородов. Сущность: проводят дегидрирование этилбензола в системе, содержащей реактор с псевдоожиженным слоем и регенератор, с использованием катализатора на основе оксида железа, нанесенного на модифицированный кремнием оксид алюминия и содержащего промоторы, представляющие собой дополнительные оксиды металлов. Технический результат: упрощение технологии. 17 з.п.ф-лы, 3 табл., 1 ил.

Способ восстановления активности цеолитсодержащего катализатора

Изобретение относится к способу восстановления активности цеолитсодержащего катализатора процесса изодепарафинизации дизельного топлива в присутствии водородсодержащего газа и может быть использовано в нефтепереработке. Предлагается способ восстановления активности цеолитсодержащего катализатора при повышенных температуре и давлении, включающий стадию обработки водородсодержащим газом, при этом в качестве цеолитсодержащего катализатора используют никель-молибденовый катализатор процесса изодепарафинизации дизельного топлива, который предварительно подвергают обработке легкой углеводородной фракцией в среде циркуляционного водородсодержащего газа, с последующей двухстадийной обработкой водородсодержащим газом, при этом в качестве водородсодержащего газа используют смесь водородсодержащего газа и сероводорода при содержании сероводорода 0,2-0,4% об. Технический результат заключается в том, что способ позволяет практически полностью восстанавливать начальную активность цеолитсодержащего никель-молибденового ...

СПОСОБ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРА, ИСПОЛЬЗУЕМОГО ПРИ ДЕГИДРАТАЦИИ ГЛИЦЕРИНА

... 1. Способ регенерации вольфрамсодержащих твердофазных катализаторов с определяемым по Гаммету показателем кислотности H0 менее +2, содержащих один или несколько промоторов, выбранных из соединений группы элементов, предпочтительно включающей золото, серебро, медь, ванадий, платину, палладий, родий, рутений, самарий, церий, иттрий, скандий, лантан, цинк, магний, железо, кобальт и никель, а также их смеси, и необязательно дополнительно содержащих соединения элементов из группы, включающей литий, натрий, калий и цезий, и/или монтмориллонит или кислые цеолиты и проявляющих после использования в процессе дегидратации глицерина до акролеина пониженную активность и/или селективность по сравнению с активностью и/или селективностью до указанного использования в процессе дегидратации глицерина, заключающийся в том, что катализаторы для их регенерации подвергают воздействию окислительной или восстановительной атмосферы. ! 2. Способ по п.1, при осуществлении которого регенерируют катализаторы с определяемым ...

СПОСОБ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРА

... 1. Способ регенерации катализатора, характеризующийся тем, что отработанный катализатор из реактора вводится в первый регенератор с псевдоожиженным слоем, где он входит в контакт с потоком кислородсодержащего газа и, произвольно, с водяным паром, чтобы осуществить реакцию горения кокса при условиях регенерации, включающих диапазон температуры от 550°C до 750°C, среднее время пребывания катализатора в пределах от 0,5 мин до 6 минут при отношении пара к потоку кислородсодержащего газа по весу в пределах от 0 до 0,1, в котором полученная смесь частично восстановленного катализатора и дымового газа вводится во второй регенератор с псевдоожиженным слоем и входит в контакт с водяным паром и дополнительным потоком кислородсодержащего газа, чтобы осуществить дальнейшую реакцию регенерации при условиях регенерации, включающих диапазон температуры от 550°C до 700°C, среднее время пребывания катализатора в пределах от 3 мин до 30 мин и поток кислородсодержащего газа, при этом отношение пара к потоку ...

СПОСОБ ДЛИТЕЛЬНОГО ПРОВЕДЕНИЯ ГЕТЕРОГЕННО КАТАЛИЗИРУЕМОГО ЧАСТИЧНОГО ОКИСЛЕНИЯ В ГАЗОВОЙ ФАЗЕ ПРОПЕНА В АКРОЛЕИН

... 1. Способ длительного проведения гетерогенно катализируемого частичного окисления в газовой фазе пропена в акролеин, при котором исходную реакционную газовую смесь, содержащую пропен, молекулярный кислород и, по меньшей мере, один инертный газ-разбавитель, пропускают через находящийся при повышенной температуре катализаторный неподвижный слой, катализаторы которого выполнены так, что их активная масса содержит, по меньшей мере, один оксид мультиметалла, который содержит элементы молибден и/или вольфрам, а также, по меньшей мере, один из элементов висмут, теллур, сурьма, олово и медь, и при котором для противодействия дезактивации катализаторного неподвижного слоя в течение времени повышают температуру катализаторного неподвижного слоя, отличающийся тем, что частичное окисление в газовой фазе, по меньшей мере, один раз в календарный год прерывают и при температуре катализаторного неподвижного слоя от 250 до 550°С через катализаторный неподвижный слой пропускают содержащую молекулярный кислород ...

СПОСОБ РЕГЕНЕРАЦИИ ИСПОЛЬЗОВАННОГО КАТАЛИЗАТОРА ГИДРООЧИСТКИ

СПОСОБ ГИДРОКОНВЕРСИИ ТЯЖЕЛОГО УГЛЕВОДОРОДНОГО СЫРЬЯ В СУСПЕНЗИИ

КАТАЛИЗАТОРЫ ГИДРООБРАБОТКИ И СПОСОБЫ ИХ ИЗГОТОВЛЕНИЯ

... 1. Cистема подачи катализатора для использования в системе переработки тяжелого нефтяного сырья, содержащая:обезжиренный использованный катализатор, содержащий множество диспергированных частиц, взвешенных в углеводородной среде в виде суспензии, где данный обезжиренный катализатор содержит первый суспензионный катализатор, который был использован в операции гидрообработки, и имеет меньше чем 80%, но больше чем 10% исходной каталитической активности;свежий суспензионный катализатор, содержащий множество диспергированных частиц в углеводородной среде в виде суспензии; игде данный обезжиренный использованный катализатор присутствует в количестве, по меньшей мере, 10% от подаваемой каталитической системы.2. Система подачи катализатора по п. 1, где свежий суспензионный катализатор готовят из, по меньшей мере, одного предшествующего соединения металла VIВ группы и, необязательно, по меньшей мере, одного предшествующего соединения промотирующего металла, выбранного из металлов VIII группы, IIВ ...

СПОСОБ ИЗГОТОВЛЕНИЯ НОСИТЕЛЯ КАТАЛИЗАТОРА ИЗ ОТРАБОТАННОГО КАТАЛИЗАТОРА

... 1. Способ изготовления материала-носителя катализатора, который включает получение отработанного материала-носителя катализатора путем выщелачивания, по меньшей мере, 50 мас.% каталитических компонентов из отработанного катализатора на носителе и дробление указанного материала-носителя катализатора таким образом, чтобы часть или весь раздробленный материал был пригодным для повторного использования, предпочтительно в качестве материала-носителя катализатора. 2. Способ по п.1, в котором отработанный материал-носитель катализатора является кристаллическим, предпочтительно высокой степени кристалличности материалом-носителем катализатора. 3. Способ по п.1, дополнительно включающий стадию смешивания части или всего раздробленного материала с новым материалом-носителем катализатора, предпочтительно в котором раздробленный отработанный материал-носитель катализатора имеет первый средний размер частиц, новый материал-носитель катализатора имеет второй средний размер частиц, а комбинированный материал-носитель ...

СПОСОБ УМЕНЬШЕНИЯ ОБРАЗОВАНИЯ ПОБОЧНЫХ ПРОДУКТОВ ПРИ ПОЛУЧЕНИИ ГАЛОГЕНАЛКАНОВЫХ СОЕДИНЕНИЙ

... 1. Способ получения галогеналкановых соединений из тетрахлорида углерода и алкена, при котором образующиеся побочные продукты CClминимизированы в течение фазы запуска реакции, включающий стадию проведения реакции с железным металлическим катализатором и одним или несколькими фосфорорганическими соединениями в качестве сокатализатора.2. Способ по п.1, дополнительно включающий стадию, на которой FeClвводят в реактор после проведения фазы запуска процесса и получения количества галогеналканового соединения.3. Способ по п.2, при котором алкен выбран из группы, состоящей из винилхлорида, этилена и 2-хлорпропена.4. Способ по п.2, при котором галогеналкановые соединения выбраны из группы, состоящей из HCC-240fa, НСС-250 и НСС-360.5. Способ по п.2, при котором железный металлический катализатор обладает формой, выбранной из группы, состоящей из железного порошка, железных шариков, железной проволоки, железной стружки и их смесей.6. Способ по п.2, при котором фосфорорганический сокатализатор выбран ...

КАТАЛИТИЧЕСКОЕ ГАЗОФАЗНОЕ ФТОРИРОВАНИЕ

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

СПОСОБ ПОЛУЧЕНИЯ (МЕТ)АКРИЛОВОЙ КИСЛОТЫ ИЛИ (МЕТ)АКРОЛЕИНА

... 1. Способ получения (мет)акриловой кислоты или (мет)акролеина, включающий в себя процесс каталитического газофазного окисления для получения (мет)акриловой кислоты или (мет)акролеина подачей пропилена, пропана или изобутилена и газа, содержащего молекулярный кислород, в реактор, заполненный катализатором, где газ, содержащий молекулярный кислород, подают в реактор, заполненный катализатором, во время остановки процесса каталитического газофазного окисления. 2. Способ по п.1, в котором газ, содержащий молекулярный кислород, подают в реактор с использованием устройства, обеспечивающего безопасность для применения во время остановки процесса каталитического газофазного окисления.

HERSTELLUNG VON METALLEN UND LEGIERUNGEN UNTER VERWENDUNG VON AUS EINEM KOHLENSTOFFHALTIGEN GAS ERZEUGTEM FESTEM KOHLENSTOFF

REGENERIERUNG VON KATALYSATOREN FÜR DIE HYDRIERUNG VON KOHLENSTOFFMONOXID

Verfahren zur Herstellung von organischen Verbindungen aus Kohlenmonoxyd und Wasserstoff

Epsilon caprolactam prodn

Epsilon-Caprolactam is prepd. by contacting epsilon-caprolactone and/or a 1-4C alkyl ester of epsilon -hydroxycaproic acid with H2 and NH3 at 200-320 degrees C. with a catalyst consisting of (I) TiO2, Al2O3, Al2O3-silicon oxide and/or silicon oxide; and (II) Cu. Gives epsilon -caprolactam with high yields and selectivity without the formation of (NH4)2SO4 as by-product.

VERFAHREN ZUR REGENRATION VON MOLYBDEN ENTHALTENDEN WIRBELBETT-OXID-KATALYSATOREN

REGENERIERUNG VON TRÄGERKATALYSATOREN FÜR DIE HYDRIERUNG VON KOHLENSTOFFMONOXID

Hydrocarbon synthesis

Carbon deposits are removed from spent hydrocarbon - synthesis catalyst, e.g. iron, cobalt, nickel, molybdenum, manganese, chromium, noble metals or their oxides, without affecting their state of oxidation, by reacting it in the fluidized state with an oxidizing gas, e.g. oxygen, air, steam or carbon dioxide, at 800-2000 DEG F. and 0-100 atmospheres, and so adjusting the composition and quantity of the oxidizing gas with reference to the amount of catalyst and the carbonaceous deposit thereon to produce an atmosphere within the regeneration zone containing substantially no free oxygen and containing carbon dioxide and carbon monoxide in such amounts that the ratio of the partial pressure of CO2 to CO is equal to or less than the value given by the equation where r is the CO2 : CO partial pressure ratio and t is the temperature in DEG F., and the sum of the partial pressures of CO2 and CO is less than the value given by the equation where S is the ...

Improvements in or relating to a catalyst for the synthesis of hydrocarbons

Iron catalysts suitable for the Fischer-Tropsch synthesis, promoted with 1.3 to 13 per cent calcium oxide and minor proportions of potassia and alumina are prepared by the reduction of a mixture of ferrosoferric oxide and minor proportions of potassia and alumina, together with 1 to 10 per cent calcium oxide based on the Fe3O4, in an atmosphere of hydrogen at 450-550 DEG C. The ferrosoferric oxide may be prepared by melting iron in the form of wire or strips with high velocity streams of oxygen; thermally decomposable salts of the promoters are added and oxidation completed, when the oxidized mass is ground and reduced. Alternatively ferrosoferric oxide may be prepared by oxyhydrogen fusion of ferric oxide. Suitable proportions of potassia are 0.05 to 1 per cent K2O based on the Fe3O4; alumina is added preferably in molecular equivalent proportion to the potassia plus an excess of 1 to 2 per cent Al2O3 based on the Fe3O4.

GETTER TRAP FOR REMOVING HYDROGEN & OXYGEN

PROCESS FOR THE REGENERATION OF A DEACTIVATED HYDROCRACKING CATALYST

... 1413495 Catalyst regeneration INTERNATIONALE RESEARCH MAATSCHAPPIJ NV 11 Oct 1972 [13 Oct 1971] 46868/72 Heading BIE [Also in Division C5] Deactivated hydrocracking catalysts comprising a sulphided fluorine-containing compositions, e.g. comprising sulphided nickel, tungsten and fluorine on silica-alumina, and which have become deactivated as a consequence of having been exposed to oxygen, e.g. during oxidative regeneration, are regenerated after discontinuing the flow of hydrocarbon feed to the catalyst by (i) oxidising with an oxygen-containing gas; (ii) converting the oxidised metal components to the sulphidic form by contact with a sulphur containing gas in the presence of hydrogen; and (iii) contacting the sulphided catalyst with a fluorine-containing gas at 175‹C to 600‹C. In the examples, the catalysts are contacted with air or an oxygen/nitrogen mixture, then a hydrogen sulphide/hydrogen mixture and then difluoroethane.

Process for the activation of a catalyst

A Fischer-Tropsch catalyst is activated by a process comprising applying to the catalyst a plurality of times a procedure comprising: a) a reduction stage comprising reducing the catalyst by contact with a hydrogen-containing gas; b) an oxidation stage comprising oxidizing the catalyst by contact with an oxygen-containing gas; and c) a reduction stage comprising reducing the catalyst by contact with a hydrogen-containing gas; between successive applications of c) and a) of the aforesaid procedure, the process further comprising: d) a synthesis stage comprising contacting the catalyst at elevated temperature and pressure with a mixture comprising carbon monoxide and hydrogen under conditions such that hydrocarbons are formed, which hydrocarbons are liquid under the prevailing conditions; the duration of the synthesis stage being short relative to the time taken for the catalyst to substantially deactivate under the conditions prevailing in the synthesis stage.

PROCESS FOR THE REACTIVATION OF A CATALYST

... 1,221,975. Reactivation of metal-contaminated catalyst. GULF RESEARCH & DEVELOPMENT CO. 6 May, 1968 [16 June, 1967], No. 21313/68. Heading B1E. [Also in Division C5] A catalyst the activity of which has become diminished by employment in the treatment of a metal-containing hydrocarbon, in which treatment the metal contained in the hydrocarbon is deposited on the catalyst to produce a metal-contaminated catalyst, is reactivated by a process which comprises contacting the catalyst (without previously subjecting the catalyst to sulphiding or to high temperature oxidation) with hydrogen peroxide in the liquid phase and thereafter separating the catalyst from the hydrogen peroxide and/or the reaction products of the hydrogen peroxide. The hydrogen peroxide may be pure hydrogen peroxide but preferably is an aqueous solution thereof. Prior to contacting with hydrogen peroxide, the catalyst may be contacted with a solvent, for example benzene or naphtha, to remove oil therefrom; after separation ...

Process for regenerating spent metal catalysts

... 542,124. Regenerating catalysts. UNIVERSAL OIL PRODUCTS CO. March 13, 1940, No. 4713. Convention date, March 22, 1939. Drawings to Specification. [Class 1 (i)] Spent metal catalysts which are contaminated by the formation of sulphides are regenerated by treating With an oxidizing gas at 400‹F. cooling and contacting with moist air at a temperature not exceeding 180‹F, to convert sulphide into sulphate, precipitating hydroxide from the sulphate and reducing this with hydrogen.

Method of reactivating oxidation catalysts

A method of reactivating an oxidation catalyst containing at least one active component selected from metals of the right-hand column of Group I, the left-hand column of Group V and VI, and Group VIII of the Periodic Table of Elements, the catalyst having been deactivated by exposure to lead-containing exhaust gases with resultant deposition of lead on the catalyst, comprises treating the catalyst with an aqueous solution of a compound of the group consisting of the polycarboxylic acids and salts thereof and the hydroxy monocarboxylic acids containing not more than 4 hydroxy groups and salts thereof, separating the treated catalyst from the solution, and drying the catalyst. The catalyst may be supported on B2O3, Al2O3, TiO2, SiO2, HfO2, Al2O3-SiO2, Al2O3-ZrO2 and Al2O3-SiO2-ZrO2. Catalytic metals specified are Pt, Pd, Ir, Rh, Fe, Co, Ni, Cr, Cu, V, W, Mo, Mn, Ag, Au and mixtures thereof, e.g. Cu-Co, Cu-Fe, Cu-Cr, Ni-Cr, Co-Cr, Mn-Cr, Mn-Fe, Pt-Fe, Pt-Co, Pt-Ni, Pd-Fe, Pd-Co, Pd-Ni, Pd-Cu ...

LEACHING METALS FROM SPENT HYDROPROCESSING CATALYSTS

RECOVERING AND CLEANING CATALYSTS

Process for the treatment of spent cobalt catalysts

... 504,700. Regenerating catalysts. RUHRCHEMIE AKT.-GES. Sept. 8, 1938, No. 26275. Convention date, Sept. 25, 1937. [Class 1 (i)] Cobalt catalysts which are precipitated on kieselguhr and have been used for the synthesis of benzines from carbon monoxide and hydrogen are regenerated by dissolving in nitric acid and re-precipitating the catalytically active material, the acid containing not more than 20 per cent and preferably no more than 3-5 per cent of free nitric acid. Preferably the solvent liquor contains also the catalytically active material, e.g. cobalt nitrate. The catalysts are treated above the melting point of the solid paraffins contained in the catalyst e.g. at 70-90‹ C., the kieselguhr being readily separated by filtration &c., and the paraffins separating as an oily layer.

Improvements in or relating to the reactivation of catalysts used in hydrogenation and like processes

Catalysts comprising a suspension in oil of finely-divided nickel, such as those prepared according to Specification 478,386 are reactivated by treatment with dry or super-heated steam followed by reduction with hydrogen or other reducing gas. The temperature of reactivation may be that at which the catalyst was originally produced, e.g. 230 DEG C. Specification 370,252, [Group IV], also is referred to.

Process for the conversion of carbon monoxide with hydrogen

... 538,225. Hydrocarbons; catalysts. POTTS, H. E. (Naamlooze Vennootschap Internationale Koolwaterstoffen Synthese Maatschappij (International Hydrocarbon Synthesis Co.)). Nov. 6, 1939, No. 29430. [Class 2 (iii)] [Also in Group III] An iron catalyst for use in the preparation of hydrocarbons from mixtures of carbon monoxide and hydrogen or the high pressure hydrogenation of oils in the liquid phase is made by treating compact iron (i.e. iron in the form of pieces of which two dimensions are at least 2 mm. and 1 mm. respectively) with oxidizing gases at high temperatures, e.g. 700-900‹C., and for such a long time that the iron is completely converted into iron oxide without melting the iron or the iron oxide formed, and subsequently reducing the iron oxide to metal by treatment with reducing gases. The catalyst may be prepared from sheet iron in the form of hollow bodies, e.g. Raschig rings. The activity of the catalysts may be increased by additions of alkali metal compounds, e.g. halides, ...

A method of producing dicobalt octacarbonyl

A process for the recovery of cobalt from residues and/or wastes containing the same by converting the cobalt to cobalt oxide. Disclosed herein is a process for recovering cobalt values from cobalt-containing residues by heating the cobalt in the presence of air to form cobalt oxide which can be separated readily from water-soluble salts which may be present therewith.

Process for the recovery of catalyst in oxidation reactions with nitric acid

The catalyst used in oxidation reactions with nitric acid is recovered, after separation of the desired oxidation product, by distilling the mother liquor under reduced pressure to remove nitric acid, diluting the residue with water to pH 1.5-6.0 and passing over an acid ion exchanger (e.g. sulphonated polystyrene), thereafter taking up the catalyst from the ion exchanger with nitric acid. In the examples, Cu + V is so recovered; Cr, Mo, W and Ni are also mentioned. Specifications 572,260, 633,354 and 756,679 are referred to.

Catalysts

PROCESS FOR REGENARATING A COBALT COMPRISING FISCHER-TROPSCH CATALYST

A METHOD FOR START-UP AND OPERATION OF A FISCHER-TROPSCH REACTOR

Process for regenarating a cobalt comprising fischer-tropsch catalyst

Catalysts.

Process of regeneration of a catalyst soiled by sulphur.

Sophisticated process of reactivation applicable to catalysts of hydrogenation.

Process of catalyst regeneration of hydrogenation.

Catalysts.

A METHOD FOR START-UP AND OPERATION OF A FISCHER-TROPSCH REACTOR

Process for regenarating a cobalt comprising fischer-tropsch catalyst

Catalysts.

Process for regenarating a cobalt comprising fischer-tropsch catalyst

A METHOD FOR START-UP AND OPERATION OF A FISCHER-TROPSCH REACTOR

RECOVERY PROCEDURE OF HETEROGENEOUS CATALYSTS AND ADSORBTIONMITTELN

PROCEDURE FOR THE HYDROGENATING PROCESSING OF WITH OF THE HYDROCARBOXYLIERUNG INTRODUCTION KOBALTHALTIGEN CATALYSTS

PROCEDURE FOR THE IMPROVEMENT OF A CATALYST

A ON AN INFLAMMABLE BONDING AGENT OF BASING MIXTURE METAL CATALYST

USE FROM DISPLACED SYNGAS TO THE REGENERATION OF SCR CATALYST

ACTIVATION OF HYDROGENATION CATALYSTS OF MEANS CARBON MONOXIDE AND USE FROM CATALYSTS TO THE HYDROGENATION

PROCEDURE FOR THE PRODUCTION OF IRON AND MOLYBDENUM AND IF NECESSARY COBALT IN THE FORM OF OXIDES CONTAINING CATALYSTS

PROCEDURE FOR THE RECOVERY OF IRON ANTIMONY METALLIC OXIDE CATALYSTS.

PROCEDURES FOR THE RECOVERY OF A USED UP CATALYST OF MEANS OF A WITH OF AN ORGANIC COMPOUND STABILIZED AQUEOUS SOLUTION OF HYDROGEN PEROXIDE.

PROCEDURE FOR THE PROCESSING FROM CATALYSTS TO THE COLOURING NUMBER HYDROGENATION OF POLYTETRAHYDROFURAN AND/OR ITS ESTERS

Procedure for the separation of cobalt from the primary products of the Oxosynthese and to its reemployment in the synthesis stage

FISCHER TROPSCH PROCEDURE

FISCHER TROPSCH PROCEDURE WITH IMPROVED CATALYST RECOVERY

CARRIER CATALYST TREATMENT

Procedure for the recovery of catalysts polluted with sulfur

HIGH-ACTIVITY CATALYSTS

Process for regenerating and rejuvenating additive containing catalysts

Process for activating a hydrotreating catalyst

Method of preparation of non-pyrophoric copper-alumina catalysts

Fischer-Tropsch catalysts

A method of producing an alumina-supported cobalt catalyst for use in a Fischer-Tropsch synthesis reaction, which comprises: calcining an initial -alumina support material at a temperature to produce a modified alumina support material; impregnating the modified alumina support material with a source of cobalt; calcining the impregnated support material, activating the catalyst with a reducing gas, steam treating the activated catalyst, and activating the steam treated catalyst with a reducing gas.

CONVERSION OF SYNGAS TO DIMETHYL ETHER

Process for the reactivation of sulfur deactivated cobalt titania catalyst

PROCESS FOR THE REMOVAL OF VANADIUM-CONTAINING ACID FROM AN ACID-EXTRACTED DEACTIVATED DEMETALLIZATION CATALYST

SOLVENT EXTRACTION PROCESS

HIGH ACTIVITY GAMMA ALUMINA CATALYSTS

Provided are high activity catalysts based upon gamma alumina containing substrates impregnated with one or more catalytically active metals, which catalysts in addition contains a nanocrystalline phase of alumina of a crystallite size at the surface of less than 25A. Also provided are processes for preparing such high activity catalysts and various uses thereof.

PROCESS FOR THE DEHYDROGENATION OF ETHYLBENZENE TO STYRENE

A process is described for the dehydrogenation of ethylbenzene to styrene in a fluid-bed reactor-regenerator system, which uses a catalyst based on iron oxide supported on a modified alumina and promoted with further metal oxides.

RECOVERING METALS FROM SPENT HYDROPROCESSING CATALYSTS

A process for recovering the metal values from spent hydroprocessing catalyst particles. The metal values will include at least one metal of Group VIII of the Periodic Table and at least one metal of Group Vb or Group VIb of the Periodic Table. The spent catalyst particles are first roasted at between 400.degree.C and 600.degree.C and then contacted with a first aqueous solution of ammonia and an ammonium salt forming a first pregnant liquor. The once-leached spent hydroprocessing catalysts are contacted with a second aqueous solution of sulfur dioxide forming a second pregnant liquor. The metal values are precipitated from the second pregnant liquor with hydrogen sulfide and the precipitate is roasted with unroasted spent hydroprocessing catalysts. The metal values of Group Vb and Group VIb in the first pregnant liquor are transferred into a first organic solution by liquid ion exchange. The first organic solution is stripped by an aqueous strip solution and the metal values separated ...

PROCESS FOR SIMULTANEOUSLY CRACKING HEAVY HYDROCARBONS INTO LIGHT OILS AND PRODUCING HYDROGEN

NO-4-27580C/YT/82 A process for simultaneously cracking a heavy hydrocarbons to form light oil and producing hydrogen is described, which comprises (1) a first step wherein steam and heavy hydrocarbons are simultaneously contacted with a catalyst in a reduced state, containing iron in the form of iron oxide, to produce hydrogen, cracked gases and cracked light oils, to convert the reducedstate catalyst into an oxidized-state catalyst, and to deposit coke on the catalyst, (2) a second step wherein the oxidized-state catalyst with coke deposited thereon is contacted with an oxygen-containing gas to partially combust the coke on the catalyst, to convert the oxidizedstate catalyst into a reduced-state catalyst, and to fix a sulfur compound contained in the coke as iron sulfide with a part of the reduced-state catalyst; and (3) a third step wherein catalyst obtained from the first step, the major portion of the catalyst being recycled between the first step and second step, is contacted with ...

CATALYST REGENERATION

PROCESS FOR PREPARING A HIGH-DENSITY AND MIDDLE-POROSITY CATALYST, SUPPORTED ON A SILICEOUS MATRIX, BASED ON VANADIUM

A process for preparing a high-density and middle-po-rosity catalyst, supported on a siliceous matrix, based on vanadium, oxygen and alkali metals, wherein the V2O5 content ranges from 6 to 9% by weight, the K2O content ranges from 8.5 to 12% by weight and the particle density ranges from 0.90 to 1.40 g/cm3 and wherein furthermore: - the volume of the pores is from 0.30 to 0.70 cm3/g and the surface area is from 0.30 to 3 m2/g, the average radius of the pores being from 650 to 2200 nanometers; - the SiO2 content is equal to or lower than 75% by weight and the Fe2O3 content is equal to or higher than 0.90% by weight.

PROCESS FOR SIMULTANEOUSLY CRACKING HEAVY HYDROCARBONS INTO LIGHT OILS AND PRODUCING HYDROGEN

RECOVERING METALS FROM SPENT HYDROPROCESSING CATALYSTS

CATALYST REGENERATION

HYDROGENATION OF CARBONACEOUS MATERIAL

A METHOD OF RESTORING CATALYTIC ACTIVITY OF A SPENT HYDROPROCESSING CATALYST, A SPENT HYDROPROCESSING CATALYST HAVING RESTORED CATALYTIC ACTIVITY AND A HYDROPROCESSING PROCESS

Disclosed is method for restoring catalytic activity to a hydroprocessing catalyst that has become spent due to its use or to the deposition of carbon thereon. The method includes a carbon reduction step whereby carbon is removed from the spent hydroprocessing catalyst in a controlled manner to within a specifically defined concentration range. Following the carbon removal step, the resulting catalyst, having a reduced concentration of carbon, is subjected to a chelation treatment whereby the resulting carbon-reduced catalyst is contacted with a chelating agent and aged for a time period necessary for realizing the benefit from the controlled carbon reduction step. In a preferred embodiment, the catalyst resulting from the chelation treatment is subjected to a sulfurization treatment involving the incorporation of elemental sulfur therein and contacting therewith an olefin.

CATALYST ADDITION TO A CIRCULATING FLUIDIZED BED REACTOR

Biomass is converted into a bio-oil containing stream in a riser reactor having multiple ports for the entry of fresh catalyst. Hard coke formed during pyrolysis may be separated from the riser effluent fraction containing which contains spent catalyst, soft coke and char. The separated hard coke may then be fed back into the riser reactor. The riser reactor may further have a cooling media which quenches the rapid heat transfer to the biomass during pyrolysis of the biomass in the mixing zone of the riser.

FISCHER-TROPSCH PROCESS

There is provided an improved system and process for the catalytic hydrogenation of carbon monoxide to form a mixture of hydrocarbons utilizing a plurality of reactors in series. Synthesis gas entering the system under pressure is partially converted in at least one initial stage reactor and the effluent therefrom introduced into a final stage reactor. In the at least one initial stage reactor, a portion of the catalyst is continuously or periodically removed with some hydrocarbons and treated to renew, or renew and enhance it, and returned. The treatment comprises reducing the hydrocarbon context of the withdrawn mixture, heating to a temperature above at least one of the metals in the catalyst thereby forming a melt, removing any slag forming on the melt, cooling the melt and reducing the particle size of the resulting solid to a fine powder of renewed catalyst. The renewed catalyst may be treated to further enhance its properties by slurry low temperature oxidation or passivated before ...

ON-LINE REGENERATION OF HYDRODESULFURIZATION CATALYST

HYDROGEN PRODUCTION USING COMPLEX METAL OXIDE PELLETS

Complex metal oxide-containing pellets and their use for producing hydrogen. The complex metal oxide-containing pellets are suitable for use in a fixed bed reactor due to sufficient crush strength. The complex metal oxide-containing pellets comprise one or more complex metal oxides and at least one of in-situ formed calcium titanate and calcium aluminate. calcium titanate and calcium alurninate are formed by reaction of suitable precursors in a mixture with one or more complex metal carbonates. The complex metal oxide-containing pellets optionally comprise at least one precious metal.

METHODS, SYSTEMS, AND APPARATUSES TO IMPROVE PROCESSES OF INCREASING FISCHER-TROPSCH CATALYST ACTIVITY

One or more embodiments of the present disclosure include methods of improving the activity of an at least partially non-active Fischer-Tropsch ("FT") catalyst in a tubular FT reactor, which includes heating a heat transfer fluid ("HTF") to a vapor state, using the heated HTF in the vapor state to achieve and maintain the at least partially non-active FT catalyst at a predetermined stage temperature; and exposing the at least partially non-active FT catalyst to at least one stage FT catalyst activity-related gas for a stage duration of time to increase the activity of the FT catalyst to a desired level. Other methods, systems and apparatuses are also disclosed.

HEAVY OIL UPGRADE PROCESS INCLUDING RECOVERY OF SPENT CATALYST

... ²²A process to upgrade heavy oil and convert the heavy oil into lower boiling ²hydrocarbon ²products is provided. The process employs a catalyst slurry comprising ²catalyst particles with an ²average particle size ranging from 1 to 20 microns. In the upgrade process, ²spent slurry catalyst in ²heavy oil is generated as an effluent stream. In one aspect, the process ²further includes the recovery of ²spent catalyst by separating heavy oil from catalyst particles in the slurry. ²In one embodiment, slurry ²catalyst in heavy oil is combined with solvent to form a combined slurry-²solvent stream. The combined ²slurry-solvent stream is filtered in a deoiling zone using membrane ²filtration. Hydrocarbons, i.e., ²solvent and residual heavy oil, can be subsequently separated from catalyst ²particles in a drying zone. ²Valuable metals can be recovered from catalyst particles for subsequent re-use ²in a catalyst synthesis ²unit, generating fresh slurry catalyst.² ...

PROCESS FOR LIMITING GAS EMISSIONS FROM POROUS PARTICLES

La présente invention a pour objet un procédé pour limiter les émissions de gaz à partir d'un matériau poreux sous forme de particules comprenant un support inorganique poreux et au moins 0,1% en poids d'un ou plusieurs composés choisi parmi les composés organiques, les composés halogénés, les composés borés et les composés phosphorés. Les particules sont placées en mouvement au sein d'un flux de gaz chaud les traversant, et une composition liquide contenant un ou plusieurs polymère(s) filmogène(s) est pulvérisée sur les particules en mouvement au moyen d'une buse d'atomisation bi-fluide dans laquelle la composition liquide est mélangée avec un gaz sous pression, avec une pression relative d'atomisation supérieure ou égale à 0,7.10 5 Pa, jusqu'a l'obtention sur la surface desdites particules d'une couche protectrice contenant le (les) polymère(s) filmogène(s) et présentant une épaisseur moyenne inférieure ou égale à 20 µm. La présente invention a également !pour objet un matériau sous forme de particules recouvertes d'une couche protectrice, susceptible d'être obtenu par ce procédé. The present invention relates to a method for limiting the gas emissions from a porous material in the form of particles comprising a porous inorganic support and at least 0.1% by weight of one or more compounds chosen from organic compounds. , halogenated compounds, boron compounds and phosphorus compounds. The particles are placed in motion within a flow of hot gas therethrough, and a liquid composition containing one or more film-forming polymer (s) is sprayed onto the moving particles by means of an atomizing nozzle. bi-fluid in which the liquid composition is mixed with a gas under pressure, with a relative atomization pressure of greater than or equal to 0.7 × 10 5 Pa, until a protective layer is obtained on the surface of said particles; the polymer (s) film-forming (s) and having an average thickness less than or equal to 20 microns. ...

REGENERATION OF A HETEROGENEOUS CATALYST USED IN ETHENE OLIGOMERIZATION

The invention relates to the in situ regeneration of heterogeneous oligomerization catalysts which are used in the liquid phase oligomenzation of ethene.

CATALYST WHICH CAN BE USED IN HYDROTREATMENT AND WHICH INCLUDES GROUP VIII METALS AND GROUP VIB METALS, AND PREPARATION THEREOF USING CITRIC ACID AND C1-C4 DIALKYL SUCCINATE

L'invention concerne un catalyseur qui comprend un support amorphe à base d'alumine, un succinate de dialkyle C1-C4, de l'acide citrique et éventuellement l'acide acétique, du phosphore et une fonction hydro-deshydrogénante comprenant au moins un élément du groupe VIII et au moins un élément du groupe VTB, catalyseur dont le spectre Raman comprend les bandes les plus intenses caractéristiques des hétéropolyanions de Keggin (974 et/ou 990 cm-1), du succinate de dialkyle C1-C4 et de l'acide citrique (notamment 785 et 956 cm-1). L'invention concerne également le procédé de préparation dudit catalyseur dans lequel un précurseur catalytique à l'état séché, calciné ou régénéré contenant les éléments de la fonction hydro-déshydrogénante, éventuellement du phosphore, est imprégné par une solution d'imprégnation comprenant au moins un succinate de dialkyle C1-C4, l'acide citrique, et éventuellement au moins un composé de phosphore et éventuellement l'acide acétique, puis est séché. L'invention concerne ...

REGENERATION OF CATALYST FOR HYDROGENATION OF SUGARS

A process for regenerating catalysts that have been deactivated or poisoned during hydrogenation of biomass, sugars and polysaccharides is described, in which polymerized species that have agglomerated to catalyst surfaces can be removed by means of washing the catalyst with hot water at subcritical temperatures. A feature of the process regenerates the catalysts in situ, which allows the process to be adapted for used in continuous throughput reactor systems. Also described is a continuous hydrogenation process that incorporated the present regeneration process.

Method for Drying Regenerated Catalyst in Route to a Propane Dehydrogenation Reactor

An apparatus and process are presented for drying a catalyst in a reactor-regenerator system. The process includes a continuous operating system with catalyst circulating between a reactor and regenerator, and the catalyst is dried before returning the catalyst to the reactor. The process uses air that is split between the drying stage and the combustion stage without adding equipment outside of the regenerator, minimizing energy, capital cost, and space requirements.

Regenerated hydrotreatment catalyst

The present invention relates to a regenerated hydrotreatment catalyst regenerated from a hydrotreatment catalyst for treating a petroleum fraction, the hydrotreatment catalyst being prepared by supporting molybdenum and at least one species selected from metals of Groups 8 to 10 of the Periodic Table on an inorganic carrier containing an aluminum oxide, wherein a residual carbon content is in the range of 0.15 mass % to 3.0 mass %, a peak intensity of a molybdenum composite metal oxide with respect to an intensity of a base peak is in the range of 0.60 to 1.10 in an X-Ray diffraction spectrum, and a peak intensity of a Mo—S bond derived from a residual sulfur peak with respect to an intensity of a base peak is in the range of 0.10 to 0.60 in a radial distribution curve obtained from an extended X-ray absorption fine structure spectrum of an X-ray absorption fine structure analysis.

Process for reprocessing spent catalysts

The invention relates to a process for reprocessing spent catalysts comprising rare earth metals, and to a process for producing a new styrene catalyst from a spent styrene catalyst.

SLURRY CATALYST AND SLURRY FLAKES VALORIZATION

The instant invention discloses a method for the valorization of spent catalyst from hydrocarbon processing slurry reactors as well as slurry flakes. 1. A method for recycling molybdenum , vanadium and nickel contained in a spent catalyst and/or a metal containing hydrocarbon feedstock , wherein said spent catalyst and/or metal containing hydrocarbon feedstock successively undergoes (i) calcination performed so as to collect carbon monoxide and hydrogen and to remove carbon containing material , (ii) washing with water , (iii) acidification with sulfuric acid to obtain an acidic water and a first precipitate which is separated , (iv) alkalinization of said acidic water with sodium hydroxide to obtain an alkaline water and a second precipitate which is separated.2. A method according to claim 1 , wherein iron chlorosulfate (FeCl(SO)) is added at steps (iii) and (iv).3. A method according to claim 1 , wherein (v) said alkaline water is further neutralized with an acid.4. A method according to claim 1 , wherein first and/or second precipitate is introduced into melted iron to obtain vanadium pentoxide (VO) claim 1 , and iron-molybdenum-nickel alloy.5. A method according to claim 1 , wherein said spent catalyst and/or metal containing hydrocarbon feedstock is obtained by the treatment of a metal containing hydrocarbon feedstock issued from an industrial unit using a metal containing catalyst claim 1 , and wherein before step (i) said spent catalyst and/or metal containing hydrocarbon feedstock are collected and treated to produce carbon monoxide claim 1 , hydrogen and a metal containing residue claim 1 , said metal containing residue being processed by steps (i) to (iv).6. A method according to claim 5 , wherein the treatment of said spent catalyst and/or metal containing hydrocarbon feedstock before step (i) is a calcination.7. A method according to claim 6 , wherein the treatment is a calcination under partial oxidation conditions.8. A method according to claim 5 , ...

Process for hydrotreating a hydrocarbon cut with a boiling point of more than 250°c in the presence of a sulphide catalyst prepared using a cyclic oligosaccharide

Preparation of a catalyst having at least one metal from group VIII, at least one metal from group VIB and at least one support; in succession: i) one of i1) contacting a pre-catalyst with metal from group VIII, metal from group VIB and support with a cyclic oligosaccharide naming at least 6 α-(1,4)-bonded glucopyranose subunits; i2) contacting support with a solution containing a precursor of metal from group VIII, a precursor of said metal from group VIB and a cyclic oligosaccharide composed of at least 6 α-(1,4)-bonded glucopyranose subunits; or i3) contacting support with a cyclic oligosaccharide composed of at least 6 α-(1,4)-bonded glucopyranose subunits followed by contacting solid derived therefrom with a precursor of metal from group VIII and a precursor of metal from group VIB.

Fischer-tropsch catalyst regeneration

A process for the regeneration of deactivated catalyst from a Fischer-Tropsch synthesis reactor, the catalyst being a supported cobalt catalyst. The process comprises the following steps: a withdrawal step, in which a portion of deactivated catalyst together with liquid hydrocarbon is withdrawn from the reactor; a concentration step, in which the concentration of the catalyst in the liquid hydrocarbon is increased; a calcination step, in which the deactivated catalyst composition is subjected to an oxidising gas to oxidise carbonaceous material contained in the deactivated catalyst in to gaseous oxides of the components of the carbonaceous material; and a reactivation step, in which the deactivated catalyst composition is reactivated to produced a regenerated catalyst.

METHOD OF PRODUCING REGENERATED HYDROTREATING CATALYST AND METHOD OF PRODUCING PETROLEUM PRODUCTS

A method of producing a regenerated hydrotreating catalyst, including a first step of preparing a hydrotreating catalyst that has been used for hydrotreatment of a petroleum fraction and has a metal element selected from Group 6 elements of the periodic table; a second step of performing regeneration treatment for part of the catalyst prepared in the first step, then performing X-ray absorption fine structure analysis for the catalyst after the regeneration treatment, and obtaining regeneration treatment conditions in which a ratio IS/IO of a peak intensity IS of a peak attributed to a bond between the metal element and a sulfur atom to a peak intensity IO of a peak attributed to a bond between the metal element and an oxygen atom is in the range of 0.1 to 0.3 in a radial distribution curve obtained from an extended X-ray absorption fine structure spectrum. 1. A method of producing a regenerated hydrotreating catalyst , comprising:a first step of preparing a hydrotreating catalyst that has been used for hydrotreatment of a petroleum fraction and has a metal element selected from Group 6 elements of the periodic table;{'sub': S', 'O', 'S', 'O, 'a second step of performing regeneration treatment for part of the catalyst prepared in the first step, then performing X-ray absorption fine structure analysis for the catalyst after the regeneration treatment, and obtaining regeneration treatment conditions in which a ratio I/Iof a peak intensity Iof a peak attributed to a bond between the metal element and a sulfur atom to a peak intensity Iof a peak attributed to a bond between the metal element and an oxygen atom is in the range of 0.1 to 0.3 in a radial distribution curve obtained from an extended X-ray absorption fine structure spectrum; and'}a third step of performing regeneration treatment under regeneration treatment conditions determined based on the second step, for the other part of the catalyst prepared in the first step.2. The method of producing a regenerated ...

Method for regenerating and hydrogenation catalyst

Disclosed is a method for regenerating a hydrogenation catalyst. More specifically, disclosed is a method for regenerating a hydrogenation catalyst poisoned during hydrogenation of a hydroformylation product for preparation of alcohol by stopping hydrogenation in a hydrogenation stationary phase reactor in which the hydrogenation catalyst is set and flowing hydrogen gas under a high temperature normal pressure. The method has an effect in that the poisoned hydrogenation catalyst can be efficiently recovered through a simple process.

Regeneration or remanufacturing catalyst for hydrogenation processing heavy oil, and method for manufacturing same

Provided are a regenerated or remanufactured catalyst for hydrogenating heavy oil or residual oil obtained by effectively removing a sulfur component, a carbonaceous component and a vanadium component, which are present in a spent catalyst for hydrogenating the heavy oil or residual oil and thus degrade an activity thereof, a method of manufacturing the same, and a method of hydrogenating heavy oil or residual oil using the same.

REDUCTION OF GREENHOUSE GAS EMISSION

Herein disclosed is a method of reducing greenhouse gas (GHG) emission comprising introducing one or more feed streams into a reformer to generate synthesis gas; and converting synthesis gas to dimethyl ether (DME). In some cases, the reformer is a fluidized bed dry reforming reactor. In some cases, the reformer comprises a hydrogen membrane. In some cases, the hydrogen membrane removes hydrogen contained in the synthesis gas and shifts reforming reactions toward completion. 1. A method of reducing greenhouse gas (GHG) emission comprisingintroducing one or more feed streams into a reformer to generate synthesis gas; andconverting synthesis gas to dimethyl ether (DME).2. The method of wherein said reformer is a fluidized bed dry reforming reactor.3. The method of wherein the reformer comprises a hydrogen membrane or a hydrogen membrane coated with an erosion resistant layer.4. The method of wherein said hydrogen membrane removes hydrogen contained in the synthesis gas and shifts reforming reactions toward completion.5. The method of wherein reformed gas exits the top of the reformer and is separated from spent catalyst.6. The method of wherein spent catalyst is routed to a regenerator in which the catalyst is regenerated.7. The method of wherein a renewable fuel is used in the regenerator.8. The method of wherein the renewable fuel comprises landfill gas claim 7 , bio-digester gas claim 7 , pyrolysis oils and liquid fuels claim 7 , spent glycerol claim 7 , biomass derived syngas claim 7 , bio-ethanol.9. The method of wherein the regenerator comprises an air pre-heater and the method utilizes full or partial displacement of natural gas or natural gas derived syngas with a bio-genic gaseous or liquid fuel in the air pre-heater.10. The method of comprising using full or partial displacement of natural gas or natural gas derived syngas with a bio-genic gaseous or liquid fuel in the regenerator.11. The method of wherein the renewable fuel used in the regenerator comprises ...

Catalyst activation method for fischer-tropsch synthesis

The present invention relates to: a catalyst activation method for Fischer-Tropsch synthesis; a catalyst regeneration method for Fischer-Tropsch synthesis; and a method for producing a liquid or solid hydrocarbon by using the Fischer-Tropsch synthesis reaction. The temperatures required for a metal carbide producing and activating reaction is markedly lower than existing catalyst activation temperatures, and the catalyst can be activated under conditions that are the same as Fischer-Tropsch synthesis reaction conditions, and thus there is no need for separate reduction equipment in the reactor, and a Fischer-Tropsch synthesis catalyst which has been used for a long time can be regenerated within the reactor without the catalyst being isolated or extracted from the reactor.

METHOD OF TREATMENT FOR A CATALYTIC REACTOR

Process for treating a catalytic reactor comprising a catalyst bed that includes the successive steps of passivating the catalytic reactor leading to the production of an oxidation layer at the surface of the active sites of the catalyst bed, opening the reactor, and skimming at least one portion of the catalyst bed. 19-. (canceled)10. A process for treating a catalytic reactor comprising a catalyst bed , comprising the sequential steps of:a) passivating the catalyst bed thereby resulting in production of an oxidation layer at a surface of active sites of the catalyst bed, said passivating step comprising the sub-steps of: i) introducing an inert gas into the catalytic reactor, the inert gas including an oxidizer at a concentration of between 50 and 100 ppm, and ii) repeating sub-step (i) with an increase of the concentration of the oxidizer in the inert gas by a factor of 2 to 10 until an oxygen concentration within the reactor is equal to an oxygen concentration in the atmosphere outside the reactor;b) opening the reactor; andc) skimming at least one portion of the catalyst bed.11. The process of claim 10 , wherein performance of said process results in an oxidation layer thickness of between 0.3 and 10 nm claim 10 , preferably of between 0.3 and 3 nm.12. The process of claim 11 , wherein performance of said process results in an oxidation layer thickness of between 0.3 and 3 nm.13. The process of claim 10 , wherein said step of passivating is carried out at a temperature of less than 200° C. claim 10 , preferably of less than 100° C.14. The process of claim 13 , wherein said step of passivating is carried out at a temperature of less than 100° C.15. The process of claim 10 , wherein said step of passivating is carried out at a pressure of less than 10 atm.16. The process of claim 15 , wherein said step of passivating is carried out at a pressure of less than 5 atm.17. The process of claim 10 , wherein said step of introducing the inert gas results in oxidation of ...

METHOD FOR REGENERATING A CATALYST WHICH IS SPENT AND REGENERATED BY A HYDRODESULFURIZATION PROCESS OF GASOLINES

A process for rejuvenating an at least partially spent catalyst resulting from a hydrodesulfurization process of a sulfur-containing olefinic gasoline cut, where the at least partially spent catalyst result is from a fresh catalyst a metal from group VIII, a metal from group VIb, and an oxide support, where the process includes 1. A process for the rejuvenation of an at least partially spent catalyst resulting from a process for the hydrodesulfurization of a sulfur-containing olefinic gasoline cut , said at least partially spent catalyst resulting from a fresh catalyst comprising at least one metal from group VIII , at least one metal from group VIb , an oxide support , and optionally phosphorus , said process comprising the following stages:a) the at least partially spent catalyst is regenerated in an oxygen-containing gas stream at a temperature of between 350° C. and 550° C. so as to obtain a regenerated catalyst,b) the regenerated catalyst is brought into contact with at least one impregnation solution containing at least one compound comprising a metal from group VIb, the molar ratio of the metal from group VIb added per metal from group VIb already present in the regenerated catalyst being between 0.15 and 2.5 mol/mol,c) a drying stage is carried out at a temperature of less than 200° C. so as to obtain a rejuvenated catalyst.2. The process as claimed in claim 1 , in which claim 1 , in stage b) claim 1 , the impregnation solution additionally contains a compound comprising a metal from group VIII; the molar ratio of the metal from group VIII added per metal from group VIII already present in the regenerated catalyst is between 0.1 and 2.5 mol/mol.3. The process as claimed in claim 1 , in which claim 1 , in stage b) claim 1 , the impregnation solution additionally contains phosphorus; the molar ratio of the phosphorus added per metal from group VIb already present in the regenerated catalyst is between 0.1 and 2.5 mol/mol.4. The process as claimed in claim 1 , ...

METHOD FOR SYNTHESIS OF COPPER/COPPER OXIDE NANOCRYSTALS

A simple approach to produce mixed Cu/CuO nanocrystals having a specific morphology by controlling the reaction temperature during Cu/CuO nanocrystals synthesis. Other variables are kept constant, such as the amount of reactants, while the reaction temperatures is maintained at a predetermined temperature of 70° C., 30° C. or 0° C., which are used to produce different and controlled morphologies for the Cu/CuO nanocrystals. The reaction mixture includes a copper ion contributor, a capping agent, a pH adjustor, and reducing agent. The reaction mixture is held at the predetermined temperature for three hours to produce the Cu/CuO nanocrystals. The synthesis method has advantages such as mass production, easy operation, and high reproducibility. 1. A method of producing CuO/Cu nanocrystals , comprising:providing 70-90 ml of a solvent,dissolving copper (II) chloride dihydrate in the solvent to provide a molar concentration of 9-11 mM of copper (II) chloride dihydrate in the solvent, dissolving polyvinylpyrrolidone with an average molecular weight of 35,000-45,000 g/mol in the solvent to provide a molar concentration of 0.02-0.06 mM of polyvinylpyrrolidone in the solvent, adding 9-11 mL of 0.1-0.3 M sodium hydroxide aqueous solution to the solvent, and adding 9-11 mL of 0.4-0.8 M L-ascorbic acid solution to the solvent to thereby form a reaction mixture, and{'sub': '2', 'stirring the reaction mixture at a predetermined temperature for two to four hours to thereby precipitate CuO/Cu nanocrystals,'}wherein the predetermined temperature is from 65° C. to 75° C., from 25° C. to 35° C., or from −5° C. to 5° C.2. The method according to claim 1 , wherein the predetermined temperature is from 65° C. to 75° C.3. The method according to claim 2 , wherein the predetermined temperature is from 69° C. to 71° C.4. The method according to claim 2 , wherein the CuO/Cu nanocrystals have an average size of from 770 nm to 870 nm.5. The method according to claim 2 , wherein the CuO/Cu ...

COMPOSITIONS FOR HIGH TEMPERATURE CATALYSIS

Ceramic compositions with catalytic activity are provided, along with methods for using such catalytic ceramic compositions. The ceramic compositions correspond to compositions that can acquire increased catalytic activity by cyclic exposure of the ceramic composition to reducing and oxidizing environments at a sufficiently elevated temperature. The ceramic compositions can be beneficial for use as catalysts in reaction environments involving swings of temperature and/or pressure conditions, such as a reverse flow reaction environment. Based on cyclic exposure to oxidizing and reducing conditions, the surface of the ceramic composition can be converted from a substantially fully oxidized state to various states including at least some dopant metal particles supported on a structural oxide surface. 1. A method for reforming a hydrocarbon-containing stream , comprising:exposing an initial composition comprising 0.1 wt % or more of at least one dopant metal oxide and 50 wt % to 99 wt % of one or more structural oxides, to a reducing environment comprising a temperature of 500° C. to 1400° C. to form a catalyst composition comprising dopant metal particles supported on the one or more structural oxides, the one or more dopant metals corresponding to dopant metal oxides having a Gibbs free energy of formation at 800° C. that is greater than a Gibbs free energy of formation at 800° C. for the one or more structural oxides by 200 kJ/mol or more, the particles of the one or more dopant metals having an average characteristic length of 10 μm or less, the dopant metal oxide comprising an oxide of Ni, Rh, Ru, Pd, Pt, Ir, or a combination thereof;exposing the catalyst composition to an oxidizing environment comprising a temperature of 500° C. to 1400° C.;{'sub': 2', '2', '2, 'exposing a hydrocarbon-containing stream to the catalyst composition in the presence of at least one of HO and COunder reforming conditions comprising a temperature of 500° C. or more to form a reformed ...

Process for rejuvenating hydrotreating catalysts

The invention refers to a process for rejuvenating a hydrotreating catalyst comprising a group VIB hydrogenation metal and/or a group VIII hydrogenation metal, which comprises the steps of: (a) regenerating the catalyst by contacting said catalyst with an oxygen containing gas at a temperature from about 300° C. to 550° C. to obtain a regenerated carbon-reduced catalyst, (b) impregnating the regenerated carbon-reduced catalyst with a solution which consists of a mixture of water and citric acid, (c) aging the impregnated catalyst for at least 6 hours and (d) drying the aged catalyst. The invention also refers to the rejuvenated catalyst obtained and its use for hydrotreating hydrocarbon feedstocks.

PROCESS FOR REJUVENATING HYDROTREATING CATALYST

The invention refers to a process for rejuvenating a hydrotreating catalyst comprising a group VIB hydrogenation metal and/or a group VIII hydrogenation metal, which comprises the steps of: (a) regenerating the catalyst by contacting said catalyst with an oxygen containing gas at a temperature from about 300° C. to 550° C., (b) impregnating the regenerated carbon-reduced catalyst with an impregnation solution which comprises a mixture of water and a combination of MoOand HPO, (c) aging the impregnated catalyst and (d) drying the aged catalyst. The invention also refers to the rejuvenated catalyst obtained and its use for hydro-treating hydrocarbon feedstocks. 1. A process for rejuvenating a hydrotreating catalyst comprising a group VIB hydrogenation metal and/or a group VIII hydrogenation metal , which comprises the steps of:a) regenerating the catalyst by contacting said catalyst with an oxygen containing gas at a temperature from about 300° C. to 550° C.,{'sub': 3', '3', '4, 'b) impregnating the regenerated carbon-reduced catalyst with an impregnation solution comprising a mixture water and a combination of MoOand HPO,'}c) aging the impregnated catalyst andd) drying the aged catalyst.2. The process according to claim 1 , wherein the temperature of the drying step d) is comprised from 80° C. to 200° C. and preferably is about 120° C.3. The process according to any of the preceding claims claim 1 , wherein the content of carbon at the end of the regeneration step a) is inferior to 0.5 wt % based on the total weight of the catalyst.4. The process according to any of the preceding claims claim 1 , wherein the concentration of MoOis comprised from 0.10 mol of MoO/mol of hydrogenation metals to 1.0 mol of MoO/mol of hydrogenation metals.5. The process according to any of the preceding claims claim 1 , wherein the concentration of HPOis comprised from 0.10 mol of HPO/mol of hydrogenation metals to 1.0 mol of HPO/mol of hydrogenation metals.6. The process according to any ...

PROCESS FOR THE HYDROSULFURIZATION OF SULFUR-CONTAINING OLEFINIC GASOLINE CUTS USING A REGENERATED CATALYST HAVING AN ORGANIC COMPOUND

The invention relates to a process for the hydrodesulfurization of a sulfur-containing olefinic gasoline cut in which said gasoline cut, hydrogen and a rejuvenated catalyst are brought into contact, said hydrodesulfurization process being carried out at a temperature of between 200° C. and 400° C., a total pressure of between 1 and 3 MPa, an hourly space velocity, defined as being the flow rate by volume of feedstock relative to the volume of catalyst, of between 1 and 10 hand a hydrogen/gasoline feedstock ratio by volume of between 100 and 1200 Sl/l, said rejuvenated catalyst resulting from a hydrotreating process and comprises at least one metal from group VIII, at least one metal from group VIb, an oxide support and at least one organic compound containing oxygen and/or nitrogen and/or sulfur. 1. A process for the hydrodesulfurization of a sulfur-containing olefinic gasoline cut in which said gasoline cut , hydrogen and a rejuvenated catalyst are brought into contact , said hydrodesulfurization process being carried out at a temperature of between 200° C. and 400° C. , a total pressure of between 1 and 3 MPa , an hourly space velocity , defined as being the flow rate by volume of feedstock relative to the volume of catalyst , of between 1 and 10 hand a hydrogen/gasoline feedstock ratio by volume of between 100 and 1200 Sl/l , said rejuvenated catalyst resulting from a hydrotreating process and comprises at least one metal from group VIII , at least one metal from group VIb , an oxide support and at least one organic compound containing oxygen and/or nitrogen and/or sulfur.2. The process as claimed in claim 1 , in which the organic compound containing oxygen and/or nitrogen and/or sulfur is chosen from a compound comprising one or more chemical functional groups chosen from a carboxylic claim 1 , alcohol claim 1 , thiol claim 1 , thioether claim 1 , sulfone claim 1 , sulfoxide claim 1 , ether claim 1 , aldehyde claim 1 , ketone claim 1 , ester claim 1 , carbonate ...

Reactivated Hydroprocessing Catalysts for Use in Sulfur Abatement

Disclosed herein are methods, systems, and compositions for providing catalysts for tail gas clean up in sulfur recovery operations. Aspects of the disclosure involve obtaining catalyst that was used in a first process, which is not a tailgas treating process and then using the so-obtained catalyst in a tailgas treating process. For example, the catalyst may originally be a hydroprocessing catalyst. A beneficial aspect of the disclosed methods and systems is that the re-use of spent hydroprocessing catalyst reduces hazardous waste generation by operators from spent catalyst disposal. Ultimately, this helps reduce the environmental impact of the catalyst life cycle. The disclosed methods and systems also provide an economically attractive source of high-performance catalyst for tailgas treatment, which benefits the spent catalyst generator, the catalyst provider, and the catalyst consumer. 1. A method of forming a reactivated catalyst for a tailgas treating process , the method comprising:obtaining a spent catalyst from a hydrotreating process, andreactivating the catalyst to form the reactivated catalyst, wherein{'sub': 2', '2', '2', '2, 'the reactivated catalyst, when contacted with a gas stream comprising one or more sulfur-containing species selected from the group consisting of elemental sulfur (Sx), sulfur dioxide (SO), carbonyl sulfide (COS), and carbon disulfide (CS), is capable of catalyzing the conversion of the one or more sulfur-containing species to hydrogen sulfide (HS) in the presence of hydrogen (H).'}2. The method of claim 1 , wherein the hydrotreating process is selected from the group consisting of petroleum hydrotreating processes claim 1 , hydrodesulfurization (HDS) claim 1 , hydrodenitrogenation (HDN) claim 1 , hydrogenation claim 1 , hydrodemetallization (HDM) claim 1 , naphtha hydrotreating (NHT) claim 1 , diesel hydrotreating (DHT) claim 1 , kerosene hydrotreating (KHT) claim 1 , jet fuel hydrotreating (JHT) claim 1 , atmospheric gas oil ...

PROCESS FOR REJUVENATION OF A USED HYDROTREATING CATALYST

The invention provides a process for rejuvenation of a used hydrotreating catalyst comprising at least 8% wt of coke and one or more non-noble Group VIII and/or Group VIb metals, which process comprises the steps of: (i) removing coke from the used hydrotreating catalyst; and (ii) treating the catalyst obtained in step (i) with of from 2 to 60% wt of gluconic acid, based on weight of dry catalyst. 1. A process for rejuvenation of a used hydrotreating catalyst comprising at least 8% wt of coke and one or more non-noble Group VIII and/or Group VIb metals , which process comprises the steps of:(i) removing coke from the used hydrotreating catalyst; and(ii) treating the catalyst obtained in step (i) with of from 2 to 60% wt of gluconic acid, based on weight of dry catalyst.2. A process according to claim 1 , in which process coke is removed by contacting the used hydrotreating catalyst with an oxygen-containing gas at a temperature of from 200 to 750° C.3. A process according to claim 1 , in which process the catalyst obtained in step (i) contains of from 0 to 10% wt of coke.4. A process according to claim 1 , in which the solution is an aqueous solution containing of from 3 to 40% wt of gluconic acid.5. A process according to claim 1 , in which the carrier is alumina.6. A process according to claim 5 , in which the carrier is gamma alumina.7. A process according to claim 1 , in which the molar ratio of compound (I) to the total Group VIB and Group VIII metal content is of from 0.01 to 2.5.8. A process for hydrotreating a sulphur-containing hydrocarbon feedstock which process comprises contacting the hydrocarbon feedstock at a hydrogen partial pressure from 1 to 70 bar and a temperature of from 200 to 420° C. with a rejuvenated catalyst as obtained according to any one of the preceding claims.9. A process according to in which the fresh hydrotreating catalyst had been obtained by(a) treating a carrier with one or more Group VIB metal components and/or one or more Group ...

Method for rejuvenating a nonregenerated spent catalyst from a process for the hydrodesulfurization of gasolines

The invention relates to a process for the rejuvenation of an at least partially spent catalyst resulting from a hydrotreating process, said at least partially spent catalyst resulting from a fresh catalyst comprising a metal from group VIII, a metal from group VIb, an oxide support, and optionally phosphorus, said at least partially spent catalyst additionally comprising carbon in a content of between 2% and 20% by weight, with respect to the total weight of the at least partially spent catalyst, and sulfur in a content of between 1% and 8% by weight, with respect to the total weight of the at least partially spent catalyst, said process comprising the following stages: a) said spent catalyst is brought into contact with an impregnation solution containing a compound comprising a metal from group VIb, b) a drying stage is carried out at a temperature of less than 200° C.

Method for rejuvenating a catalyst of a hydroprocessing and/or hydrocracking process

The invention concerns a method for rejuvenating an at least partially used catalyst originating from a hydroprocessing and/or hydrocracking process, the at least partially used catalyst being derived from a fresh catalyst comprising at least one group VIII metal (in particular, Co), at least one group VIB metal (in particular, Mo), an oxide support, and optionally phosphorus, the method comprising the steps: a) regenerating the at least partially used catalyst in a gas stream containing oxygen at a temperature between 300° C. and 550° C. so as to obtain a regenerated catalyst, b) then placing the regenerated catalyst in contact with phosphoric acid and an organic acid, each having acidity constant pKa greater than 1.5, c) performing a drying step at a temperature less than 200° C. without subsequently calcining it, so as to obtain a rejuvenated catalyst.

SUPPORTED CATALYST AND METHOD OF PRODUCING FIBROUS CARBON NANOSTRUCTURES

A supported catalyst comprises: a support that is particulate; and a composite layer laminate formed outside the support and including two or more composite layers, wherein each of the composite layers includes a catalyst portion containing a catalyst and a metal compound portion containing a metal compound, the support contains 10 mass % or more of each of Al and Si, and a volume-average particle diameter of the support is 50 μm or more and 400 μm or less. 1. A supported catalyst , comprising:a support that is particulate; anda composite layer laminate formed outside the support,wherein the composite layer laminate is composed of n composite layers, where n is an integer of 2 or more,each of the composite layers in the composite layer laminate includes a catalyst portion containing a catalyst and a metal compound portion containing a metal compound,the support contains 10 mass % or more of each of Al and Si, anda volume-average particle diameter of the support is 50 μm or more and 400 μm or less.2. The supported catalyst according to claim 1 ,wherein the metal compound portion contains 10 mass % or more of Al.3. The supported catalyst according to claim 1 ,wherein the catalyst portion contains at least metal of any of Fe, Co, and Ni.4. The supported catalyst according to any one of claim 1 ,wherein the composite layer in the composite layer laminate includes a metal compound layer which is the metal compound portion in layer form, a catalyst layer which is the catalyst portion in layer form, and/or a mixed layer in which the metal compound and the catalyst coexist.5. The supported catalyst according to claim 4 ,wherein a catalyst metal equivalent thickness of the catalyst contained in the composite layer is 0.1 nm or more and 10 nm or less per one composite layer.6. The supported catalyst according to claim 4 ,wherein a metal compound equivalent thickness of the metal compound contained in the composite layer is 1 nm or more and 1 μm or less per one composite layer ...

System and Method for Dual Fluidized Bed Gasification

A system, for production of high-quality syngas, comprising a first dual fluidized bed loop having a fluid bed conditioner operable to produce high quality syngas comprising a first percentage of components other than CO and Hfrom a gas feed, wherein the conditioner comprises an outlet for a first catalytic heat transfer stream comprising a catalytic heat transfer material and having a first temperature, and an inlet for a second catalytic heat transfer stream comprising catalytic heat transfer material and having a second temperature greater than the first temperature; a fluid bed combustor operable to combust fuel and oxidant, wherein the fluid bed combustor comprises an inlet connected with the outlet for a first catalytic heat transfer stream of the conditioner, and an outlet connected with the inlet for a second catalytic heat transfer stream of the conditioner; and a catalytic heat transfer material. 1. A method for continuous dry reforming , the method comprising:introducing a feed comprising carbon dioxide and at least one selected from methane and propane into a fluid bed conditioner operated at a conditioning temperature, wherein the fluid bed conditioner is one fluid bed of a dual fluidized bed loop and is configured to convert at least a portion of said feed into synthesis gas components;extracting a first catalytic heat transfer stream comprising a catalytic heat transfer material and having a first temperature from the fluid bed conditioner and introducing at least a portion of the first catalytic heat transfer stream and a flue gas into a fluid bed combustor, wherein the fluid bed combustor is configured to regenerate the catalyst via combustion;extracting a second catalytic heat transfer stream comprising catalytic heat transfer material and having a second temperature from the fluid bed combustor and introducing at least a portion of the second catalytic heat transfer stream into the fluid bed conditioner; andextracting synthesis gas from the fluid ...

CATALYTIC PYROLYSIS OF POLYSTYRENE INTO AROMATIC RICH LIQUID PRODUCT USING SPHERICAL CATALYST

The present invention provides a process of catalytic depolymerization of polystyrene involving a spherical catalyst, an apparatus for carrying out the depolymerization, recovering the aromatic rich liquid product and recycling the catalyst without any decrease in the catalytic performance. Further, the present invention provides that the aromatic rich liquid product includes styrene, xylene, benzene, ethyl benzene, with styrene content greater than 65%. Additionally, the catalyst involved in the depolymerization process is a spherical catalyst that is easily recovered from coke/char formed during the process and is recycled and reused without any decrease in the catalytic performance. 1. A process of catalytic depolymerization of polystyrene , the process comprising:(a) adding a polystyrene feed and a catalyst into a reactor, wherein the catalyst and the feed are added together, or the feed is added first followed by the catalyst, or the feed is added into the reactor containing the catalyst; wherein the catalyst is a spherical catalyst;(b) mixing of the feed with the catalyst in the reactor to obtain a mixture and heating the mixture at a rate ranging from 3 to 20° C./min in an inert atmosphere for generating vapor;(c) passing the vapor from the reactor to a condenser to obtain a condensate, wherein a heating tape is connected to a temperature controller in the reactor to prevent condensation of the vapor before entering the condenser; and(d) routing the condensate from the condenser to a liquid product collection flask and passing un-condensable gases from the condenser through a scrubber; wherein the liquid product is present in an amount ranging from 85% to 90% by weight comprising styrene in an amount ranging from 65% to 71% by weight of the liquid product.2. The process as claimed in claim 1 , wherein the feed is a styrene rich polymer waste comprising styrene in an amount ranging from 20% to 100% by weight claim 1 , wherein the styrene rich polymer is ...

A METHOD FOR START-UP AND OPERATION OF A FISCHER-TROPSCH REACTOR

The invention relates to a method for start-up and operation of a Fischer-Tropsch reactor comprising the steps of: (a) providing a reactor with a fixed bed of reduced Fischer-Tropsch catalyst that comprises cobalt as catalytically active metal; (b) supplying a gaseous feed stream comprising carbon monoxide and hydrogen to the reactor, wherein the gaseous feed stream initially comprises a nitrogen-containing compound other than molecular nitrogen in an initial concentration in the range of from 0.1 to 50 ppmv based on the volume of the gaseous feed stream; (c) converting carbon monoxide and hydrogen supplied with the gaseous feed stream to the reactor into hydrocarbons at an initial reaction temperature, wherein the initial reaction temperature is set at a value of at least 200° C. and hydrocarbons are produced at a first yield; (d) maintaining the initial reaction temperature at the set value and maintaining the first yield by decreasing the concentration of the nitrogen-containing compound in the gaseous feed stream supplied to the reactor; (e) optionally increasing the reaction temperature after the concentration of the nitrogen-containing compound in the gaseous feed stream has decreased to a value below 100 ppbv. 1. A method for start-up and operation of a Fischer-Tropsch reactor comprising the steps of:(a) providing a reactor with a fixed bed of reduced Fischer-Tropsch catalyst that comprises cobalt as catalytically active metal;(b) supplying a gaseous feed stream comprising carbon monoxide and hydrogen to the reactor, wherein the gaseous feed stream initially comprises a nitrogen-containing compound other than molecular nitrogen in an initial concentration in the range of from 0.1 to 50 ppmv based on the volume of the gaseous feed stream;(c) converting carbon monoxide and hydrogen supplied with the gaseous feed stream to the reactor into hydrocarbons at an initial reaction temperature, wherein the initial reaction temperature is set at a value of at least 200° ...

Process for the Oxidative Dehydrogenation of N-Butenes to Butadiene

The invention relates to a process for the oxidative dehydrogenation of n-butenes to butadiene, which comprises two or more production steps (i) and at least one regeneration step (ii), in which (i) in one production step, a starting gas mixture comprising n-butenes is mixed with an oxygen-comprising gas and brought into contact with a multimetal oxide catalyst which comprises at least molybdenum and a further metal and is arranged in a fixed catalyst bed in a fixed-bed reactor at a temperature of from 220 to 490° C., and, before the relative decrease in conversion at constant temperature is >25%, (ii) in a regeneration step, the multimetal oxide catalyst is regenerated by passing an oxygen-comprising regeneration gas mixture at a temperature of from 200 to 450° C. over the fixed catalyst bed and burning off the carbon deposited on the catalyst, where a regeneration step (ii) is carried out between two production steps (i), wherein from 2 to 50% by weight of the carbon deposited on the catalyst is burnt off per regeneration step (ii).

PROCESS FOR THE CATALYTIC PREPARATION OF HYDROGEN CYANIDE FROM METHANE AND AMMONIA

The invention relates to a catalyst material comprising a support, a first metal and a second metal on said support. The first and second metals are in the form of a chemical compound. The first metal is Fe, Co or Ni, and the second metal is selected from the group consisting of Sn, Zn and In. The invention also relates to a process for the preparation of hydrogen cyanide (HCN) from methane (CH) and ammonia (NH), wherein the methane and ammonia are contacted with a catalyst according to the invention. 1. A process for the preparation of hydrogen cyanide (HCN) from methane (CH) and ammonia (NH) , wherein the methane and ammonia are contacted with a catalyst material comprising a support , a first metal and a second metal on said support , wherein said first and second metal are in the form of a chemical compound , where said first metal is Fe , Co or Ni , and where said second metal is selected from the group consisting of Sn , Zn and In , and the temperature of the process is less than 1000° C.2. A process according to claim 1 , wherein the temperature of the process is between 750° C. and 950° C.3. A process according to claim 1 , wherein the support is a ferromagnetic support used as an inductive heating element in the process.4. A process according to claim 3 , wherein the support comprises Co and wherein the second metal is coated onto the support.5. A process according to claim 1 , wherein the support comprises an alumina claim 1 , a spinel of alumina claim 1 , an oxide claim 1 , a carbide claim 1 , a nitride claim 1 , or a carbonitride.6. A process according to claim 1 , wherein the first and second metal form a ternary compound with carbon or nitrogen.7. A process according to claim 1 , wherein the first metal comprises Co.8. A process according to claim 1 , wherein the first metal comprises Co and the second metal comprises Sn.9. A process according to claim 1 , wherein the ratio of the weight percent of Fe claim 1 , Co or Ni to Sn claim 1 , Zn or In is ...

ORGANIC WASTEWATER TREATMENT METHOD BASED ON MULTI-ELEMENT CO-DOPING TIO2 NANO PHOTOCATALYTIC MATERIAL

An organic wastewater treatment method based on a multi-element co-doping TiOnano photocatalytic material includes preparing a sulfur-titanium dioxide mixture, hydrothermally reacting the sulfur-titanium dioxide mixture with copper chloride, ammonia, strong alkali, a transition metal salt and the like, reacting the resulting reaction product with hydrofluoric acid, then performing temperature programming thermal treatment in air to obtain the multi-element co-doping TiOnano photocatalytic material, and then treating organic wastewater with the multi-element co-doping TiOnano photocatalytic material under the irradiation of visible light. The organic wastewater treatment method is efficient and rapid, safe and environmental-friendly, can thoroughly degrade many types of organic pollutants, ammonia nitrogen and the like, and does not cause secondary pollution; furthermore, the adopted multi-element co-doping TiOnano photocatalytic material can be regenerated and recycled only by simple calcination, and the cost is inexpensive. 1. An organic wastewater treatment method based on a multi-element co-doping TiOnano photocatalytic material , comprising:(1) successively adding butyl titanate and titanium disulfide into absolute ethyl alcohol, continuously stirring until a dropwise addition is completed, then dropwise adding a nitric acid solution, and stirring for 1-2 h in a water bath at 30-60° C. to obtain a sulfur-titanium dioxide mixture;(2) adding the sulfur-titanium dioxide mixture into a copper chloride solution, and successively adding an alkaline aqueous solution and a transition metal salt aqueous solution, transferring an obtained mixture into a hydrothermal reactor, and continuously reacting for 10-20 h at 150-160° C.;(3) performing a suction filtration on a reaction mixture obtained in step (2), washing an obtained filter cake to be neutral with a deionized water, drying for 1-2 h in a vacuum at 60-80° C., uniformly mixing a dried filter cake with a hydrofluoric ...

Fluidized cracking process for increasing olefin yield and catalyst composition for same

An improved process and catalyst composition for cracking hydrocarbons in a fluidized cracking process are disclosed. The process employs circulating inventory of a regenerated cracking having a minimal carbon content. The regenerated catalyst comprises a catalyst/additive composition which contains a pentasil zeolite, iron oxide, and a phosphorous compound. In accordance with the present disclosure, the catalyst/additive contains controlled amounts of iron oxide which is maintained in an oxidized state by maintaining low amounts of carbon on the regenerated catalyst inventory. In this manner it was discovered that the catalyst composition greatly enhances the production and selectivity of light hydrocarbons, such as propylene.

NANOCRYSTALLINE COMPOSITE CATALYST FOR STORING/SUPPLYING HYDROGEN, NANOCRYSTALLINE COMPOSITE CATALYST MIXTURE FOR STORING/SUPPLYING HYDROGEN, AND METHOD FOR SUPPLYING HYDROGEN

The present disclosure provides that a catalyst exhibits excellent catalytic activity in both a hydrogenation involving a hydrogen-storing body containing an aromatic compound, and a dehydrogenation involving a hydrogen-supplying body containing a hydrogen derivative of the aromatic compound, wherein the catalyst contains a nanocrystalline composite having two or more accumulated flake-like nanocrystalline pieces in a connected state, the flake-like nanocrystalline pieces each having a main surface and an end surface, and in that the nanocrystalline composite is configured such that, when two adjacent nanocrystalline pieces are viewed, an end surface of at least one of the nanocrystalline pieces is connected. 1. A nanocrystalline composite catalyst for storing/supplying hydrogen exhibiting excellent catalytic activity in both a hydrogenation involving a hydrogen-storing body containing an aromatic compound , and a dehydrogenation involving a hydrogen-supplying body containing a hydrogen derivative of the aromatic compound ,the catalyst contains a nanocrystalline composite having two or more accumulated flake-like nanocrystalline pieces in a connected state, the flake-like nanocrystalline pieces each having a main surface and an end surface; andthe nanocrystalline composite is configured such that, when two adjacent nanocrystalline pieces are viewed, an end surface of at least one of the nanocrystalline pieces is connected.2. The nanocrystalline composite catalyst for storing/supplying hydrogen according to claim 1 , wherein:the catalyst further contains a base material; andat least one nanocrystalline piece forming the nanocrystalline composite is configured to be connected to a surface of the base material.3. The nanocrystalline composite catalyst for storing/supplying hydrogen according to claim 1 , wherein the nanocrystalline composite is a nanocrystalline metal composite in which the nanocrystalline piece forming the nanocrystalline composite contains one or two ...

METHOD FOR SORTING CONTAMINATED CATALYSTS OR ADSORBENTS

A method and a device for separation of at least one catalyst and/or adsorbent from a homogeneous mixture of catalysts and/or adsorbents containing one or more metal, semi-metal or non-metal contaminant(s) deposited thereon, making it possible to separate catalysts or adsorbents according to the presence or absence of contaminant and also according to the contaminant content, starting from a sorting threshold that corresponds to a content and that is defined by the operator. 1. Method for separation of at least one catalyst and/or adsorbent from a homogeneous mixture of catalysts and/or adsorbents that are spent catalysts or adsorbents , with said catalysts or adsorbents containing one or more metal , semi-metal or non-metal contaminant(s) selected from the group that is formed by Fe , Hg , Ni , V , C , Cl , Na , S , N , Si , P , As , with said contaminant(s) being deposited on said catalyst or adsorbent grains , method in which the catalyst or adsorbent grains are separated according to a sorting threshold corresponding to a contaminant content and defined by the user , method in whichThe catalyst grains of said mixture run past an LIBS detection system that detects the wavelength that characterizes said contaminant,The analyzing device associated with LIBS processes the signal that is sent by the detection system by comparing it to a set-point value that indicates the sorting threshold,The analyzing device sends a signal for ordering the evacuation of grains according to its contaminant content, and at least 2 batches—at least one batch of catalysts or adsorbents that are heavily loaded with said contaminant in relation to the sorting threshold and at least one batch of catalysts or adsorbents that are lightly loaded with said contaminant in relation to the sorting threshold—are obtained,And the catalysts that are lightly loaded with contaminant are treated before being reused in an industrial method, and preferably said method is selected from the group that is ...

REGENERATION OF CATALYST

A catalyst is regenerated by an inventive process using a heat exchange fluid such as superheated steam to remove heat during the process relying on efficient heat transfer (e.g., enabled by the microchannel reactor construction) in comparison with prior art heat exchange relying on a phase change, e.g. between water and (partial or complete vaporization) steam, allows simplification of the protocols to enable transition at higher temperatures between steps which translates in reduced duration of the regeneration process and avoids potential water hammering risks. 2. The process according to wherein step a) is initiated upon cool-down of the reactor from synthesis (eg FT synthesis) mode to a transition temperature of approximately 170° C. for an optional nitrogen purge and the introduction of the hydrogen containing gas.3. The process according to or wherein in step a) the temperature of the catalyst bed claim 1 , of the reactor and/or of the dewaxing gas stream is raised to a temperature of 250° C. to 400° C. claim 1 , preferably to 330° C. to 380° C. claim 1 , more preferably 340° C. to 360° C. and kept at or near (preferably within 15° C. of) that holding temperature for a period of one hour to 24 hours claim 1 , preferably 10 to 20 hours claim 1 , more preferably 10 to 15 hours.5. A process in accordance with for the regeneration of a hydrocarbon processing catalyst in situ in a microchannel reactor provided with heat exchange channels.6. The process according to any one of to wherein the heat exchange fluid is steam.7. The process according to any one of to wherein the catalyst is a metal based catalyst claim 4 , for example a Fischer-Tropsch catalyst claim 4 , such as a cobalt or iron-containing catalyst.8. The process according to any one of to wherein the catalyst is disposed on a porous support.9. The process according to any one of to wherein the temperature of each gas stream is controlled by heat exchange fluid flowing through the heat exchange channels ...

RECOVERY AND RECYCLING OF BYPRODUCTS OF ACTIVATED ALUMINUM

Methods, systems, and compositions related to the recycling and/or recovery of activating materials from activated aluminum are disclosed. In one embodiment, an aqueous solution's composition may be controlled to maintain aluminum ions dissolved in solution during reaction of an activated aluminum. In another embodiment, aluminum hydroxide containing the activating materials may be dissolved into an aqueous solution to isolate the activating materials. 1. A method of reacting an activated aluminum , the method comprising:exposing the activated aluminum to an aqueous solution, wherein the activated aluminum comprises aluminum combined with gallium and/or indium;reacting the aluminum in the activated aluminum with water in the aqueous solution to generate hydrogen and aluminum ions; andmaintaining the aluminum ions dissolved in the aqueous solution during the reaction.2. The method of claim 1 , further comprising forming a separate phase comprising the gallium and/or indium.3. The method of claim 1 , further comprising combining phases comprising the gallium and/or indium into a mass.4. A method of recovering one or more activating materials claim 1 , the method comprising:adding a composition comprising aluminum hydroxide and the one or more activating materials to an aqueous solution, wherein the one or more activating materials includes at least one selected from the group of indium and gallium;dissolving the aluminum hydroxide to form aluminum ions and hydroxide ions dissolved in the aqueous solution; andforming a separate phase comprising the activating materials.5. The method of claim 4 , further comprising controlling a composition of the aqueous solution to maintain the aluminum ions dissolved in the aqueous solution.6. The method of claim 4 , further comprising combining at least two separate phases comprising the activating materials into a mass.7. The method of claim 4 , further comprising maintaining a pH of the aqueous solution to be greater than or equal ...

METHODS AND MATERIALS FOR IMPROVED CATALYTIC OLIGOMERIZATION

Described herein are materials and methods for improved catalytic oligomerization of an ethylene monomer and/or propylene monomer. The present disclosure teaches oligomerizing the ethylene monomer or propylene monomer to produce oligomers. Also described is a heterogeneous catalyst comprising sulfate modified nickel on titanium modified alumina and a surface modification with yttrium (Y) suitable for use in the disclosed oligomerization. 1. A process for the catalytic oligomerization of an ethylene monomer comprising:providing a first stream comprising ethane and ethylene monomer;providing a heterogeneous catalyst, the heterogeneous catalyst comprising sulfate modified nickel on titanium modified alumina, and a surface modification with yttrium (Y);contacting the first stream and the heterogeneous catalyst under oligomerization conditions;oligomerizing the ethylene monomer in the first stream to produce an oligomer, the oligomer comprising one or more of a butene, hexene, octene, or a heavier olefinic compound, derivatives thereof or any combination thereof; andoptionally, providing an oligomer stream, wherein the concentration of oligomer in the oligomer stream is greater than the concentration of oligomer in the first stream.2. A process for the catalytic oligomerization of a propylene monomer comprising:providing a first stream comprising propane and propylene monomer;providing a heterogeneous catalyst, the heterogeneous catalyst comprising sulfate modified nickel on titanium modified alumina, and a surface modification with yttrium (Y);contacting the first stream and the heterogeneous catalyst under oligomerization conditions;oligomerizing the propylene in the first stream to produce an oligomer, the oligomer comprising one or more of a hexene, nonene, or a heavier olefinic compound, derivatives thereof or any combination thereof; andoptionally, providing an oligomer stream, wherein the concentration of oligomer in the oligomer stream is greater than the ...

Regeneration process for metal catalyst based gas purifiers

Disclosed herein are methods for regenerating metal catalysts used in the purification of inert gases for use in fiber draw furnaces and other applications. The methods described herein can regenerate metal catalysts alone or in combination with molecular sieves. The methods disclosed herein are able to prevent the formation and retention of unwanted byproducts during and after the regeneration process, thereby efficiently converting oxidized catalysts to their reduced or elemental form. Gases purified with catalysts regenerated by the methods disclosed herein, when used in fiber draw furnaces and similar applications, can lead to extended equipment lifetimes and higher-quality products due to the lack of degradation by contaminants in the gas stream.

Method and system of elemental sulfur recycling and catalyst regenerating for sulfur-deposited catalyst

The present invention discloses a method and system of recovering elemental sulfur and regenerating the catalyst for a sulfur-deposited catalyst, including immersing the sulfur-deposited catalyst in the ammonium sulfide solution, the leaching reaction under normal pressure and temperature, replacing the ammonium sulfide solution and immersing again for extraction for the same time; collecting the leachate of the two steps, conducting gas stripping of the elemental sulfur by adopting the high-temperature nitrogen gas, condensing the tail gas of gas stripping, subjecting to a purification treatment and then discharging, with the liquor condensate being the ammonium sulfide solution. Finally, the solid in the leachate is filtered, washed and dried after the gas stripping to obtain the elemental sulfur; and the washing and drying of catalysts that has been subjected to the two times of immersion and extraction obtain the regenerated catalysts.

PHENOL ALKYLATION CATALYST PRECURSOR AND CATALYST, METHOD OF FORMING CATALYST, METHOD OF REGENERATING CATALYST, AND METHOD OF ALKYLATING PHENOL

A phenol alkylation catalyst exhibiting a desirable combination of activity, selectivity, and regenerability is prepared from a catalyst precursor that includes specific amounts of magnesium oxide, copper oxide or a copper oxide precursor, a hydrous magnesium aluminosilicate-containing binder, a pore-former, a lubricant, and water. Methods of forming and regenerating the catalyst, as well as a phenol alkylation method, are described. 1. A catalyst precursor comprising , based on the total weight of the catalyst precursor:70 to 98 weight percent magnesium oxide;0.1 to 2 weight percent copper oxide or a copper oxide precursor;0.5 to 8 weight percent a binder comprising a hydrous magnesium aluminosilicate;1 to 15 weight percent a pore-former;0.2 to 5 weight percent a lubricant; and0.2 to 15 weight percent water.2. The catalyst precursor of claim 1 , having a density of 1.2 to 2 grams per milliliter at 23° C. claim 1 , determined as described in the working examples.3. The catalyst precursor of claim 1 , wherein the magnesium oxide has a Brunauer-Emmett-Teller surface area of at least 70 meter/gram.4. The catalyst precursor of claim 1 , wherein the copper oxide or a copper oxide precursor comprises cupric oxide claim 1 , cupric nitrate claim 1 , cuprous carbonate claim 1 , a hydrate of one of the foregoing claim 1 , or a combination thereof.5. The catalyst precursor of claim 1 , wherein the pore-former comprises polyethylene glycol.6. The catalyst precursor of claim 1 , wherein the lubricant comprises graphite claim 1 , magnesium stearate claim 1 , or a combination thereof.7. The catalyst precursor of claim 1 , comprising75 to 95 weight percent of the magnesium oxide;0.2 to 1 weight percent of the copper oxide or copper oxide precursor;1 to 6 weight percent of the binder comprising a hydrous magnesium aluminosilicate;2 to 10 weight percent of the pore-former;0.4 to 3.5 weight percent of the lubricant; and0.6 to 12 weight percent of the water.8. A method of forming a ...

Presulfurized Catalyst Composition

A system and method of presulfurizing a catalyst. The presulfurizing of the catalyst includes contacting the catalyst with elemental sulfur, an olefin, and a triglyceride to form a mixture, and heating the mixture to give a presulfurized catalyst. 120-. (canceled)21. A method of hydroprocessing using a presulfided catalyst , comprising: contacting a sulfidable catalyst with sulfur, an olefin, and a triglyceride at a specified weight ratio of the olefin to the total weight of olefin and triglyceride of between 0.4 to 0.6 to form a mixture, wherein the weight ratio of the sulfur to the total weight of the catalyst is between 0.02 to 0.15;', 'heating the mixture to form a presulfurized catalyst; and', 'adding hydrogen to the presulfurized catalyst ex-situ of a hydroprocessing reactor to form the presulfided catalyst;, 'forming the presulfided catalyst byperforming an initial startup of the hydroprocessing reactor after loading of the presulfided catalyst to form a hydroprocessed hydrocarbon product;feeding hydrocarbon feed comprising cracked feedstock comprising coker naptha, coker diesel, or light cycle oil (LCO), or any combinations thereof, to the hydroprocessing reactor within first three days of the initial startup; andcatalyzing, via the presulfided catalyst, hydroprocessing of the hydrocarbon feed in the hydroprocessing reactor to give the hydroprocessed hydrocarbon product.22. The method of claim 21 , wherein the presulfurized catalyst comprises a carbonaceous barrier formed via the heating of the mixture of the sulfidable catalyst claim 21 , the sulfur claim 21 , the olefin claim 21 , and the triglyceride claim 21 , and wherein the hydroprocessing comprises hydrotreating claim 21 , hydrocracking claim 21 , or pyrolysis gasoline (pygas) treating claim 21 , or any combination thereof.23. The method of claim 21 , wherein the sulfidable catalyst comprises a metal oxide catalyst having one or more oxides of metals from Group VIE and Group VIII of the Periodic Table ...

CATALYST FOR PRODUCING HYDROCARBONS

A hydropyrolysis catalyst and a process using that catalyst are described. The catalyst comprises a support and an active metal component wherein the catalyst is an eggshell type catalyst having the active metal component located in the outer portion of the support. 1. A process for converting biomass to products comprising:a. contacting the biomass with hydrogen in the presence of a fluidized bed of fresh hydropyrolysis catalyst in a reactor vessel under hydropyrolysis conditions;b. removing products and char from the reactor vessel;c. carrying out the contacting and removing steps for a period of time such that the fresh hydropyrolysis catalyst attrits in the fluidized bed to form small catalyst particles; andd. removing at least a portion of the small catalyst particles with the products and char,wherein the fresh hydropyrolysis catalyst comprises a support and an active metal component and wherein the fresh hydropyrolysis catalyst is an eggshell catalyst having the active metal component located in the outer portion of the support; andwherein the products leave the fluidized bed at an exit bed velocity, the char has a settling velocity that is less than the exit bed velocity, the fresh hydropyrolysis catalyst has a settling velocity that is greater than the exit bed velocity, and the small catalyst particles have a settling velocity that is less than the exit bed velocity.2. A process as claimed in wherein the settling velocity of the char is less than 90% of the exit bed velocity.3. A process as claimed in wherein the settling velocity of the char is less than 75% of the exit bed velocity.4. A process as claimed in wherein the settling velocity of the fresh hydropyrolysis catalyst is greater than 110% of the exit bed velocity.5. A process as claimed in wherein the settling velocity of the fresh hydropyrolysis catalyst is greater than 150% of the exit bed velocity.6. A process as claimed in wherein the settling velocity of the small catalyst particles is less ...

CATALYTIC BIOMASS PYROLYSIS PROCESS

Described herein are processes for converting a biomass starting material (such as lignocellulosic materials) into a low oxygen containing, stable liquid intermediate that can be refined to make liquid hydrocarbon fuels. More specifically, the process can be a catalytic biomass pyrolysis process wherein an oxygen removing catalyst is employed in the reactor while the biomass is subjected to pyrolysis conditions. The stream exiting the pyrolysis reactor comprises bio-oil having a low oxygen content, and such stream may be subjected to further steps, such as separation and/or condensation to isolate the bio-oil. 132-. (canceled)33. A catalytic biomass pyrolysis system comprising:a reactor adapted for combining a biomass with a solid catalyst in a reduced state under pyrolysis conditions to form a pyrolysis product stream;a separation unit in fluid connection with the reactor and adapted to form a first stream comprising a solids fraction from the pyrolysis product stream, said solids fraction comprising non-catalyst solids and solid catalyst, at least a portion of which is in an oxidized state, and a second stream comprising a vapors fraction from the pyrolysis reaction stream;a condenser unit in fluid communication with the separation unit and adapted to condense a bio-crude from the vapors in the second stream separate from a gas component of the second stream;an optional liquid separator unit in fluid communication with the condenser unit and adapted to separate water or another liquid from the bio-crude;a catalyst regeneration unit in fluid communication with the separation unit and adapted to remove the non-catalyst solids from the solid catalyst present in the first stream;a reduction unit in fluid communication with the catalyst regeneration unit and adapted to reduce the solid catalyst that is in the oxidized state received from the catalyst regeneration unit and provide solid catalyst in a reduced state; anda catalyst delivery stream adapted to deliver the ...

Fischer-Tropsch Catalyst Performance Enhancement Process

The present invention relates to a process for treating a catalyst to improve performance, and more specifically to a process for treating a Fischer-Tropsch catalyst using a high hydrogen syngas to improve catalyst performance. 1. A process for improving performance of a Fischer-Tropsch catalyst comprising the steps of:{'sup': −1', '−1, '(a) contacting the catalyst with hydrogen or syngas at a temperature in the range of from about 200° C. to about 450° C., under a pressure in the range of from about 0 barg to about 50 barg, and a GHSV in the range of from about 500 hrto about 5000 hr, for a period of time of at least 1 hour to provide a reduced catalyst;'}{'sub': '2', 'sup': '−1', '(b) contacting the reduced catalyst of step (a) with syngas comprising H:CO in a ratio in the range of from about 1:1 to about 2.1:1, in a Fischer-Tropsch synthesis reactor under a pressure in the range of from about 0 barg to about 50 barg and a GHSV of over 1000 hr, at a temperature in the range of from about 100° C. to about 280° C.;'}{'sub': '2', 'sup': −1', '−1, '(c) increasing the ratio of H:CO of the syngas to a ratio of at least 3:1 at a pressure in the range of from about 30 barg to about 42 barg, for a period of time of at least 1 hour at a temperature in the range of from about 160° C. to about 250° C., and a GHSV in the range of from about 1000 hrto about 8000 hr; and'}{'sub': '2', 'sup': '−1', '(d) decreasing the ratio of H:CO of the syngas to a ratio in the range of from about 1:1 to about 2.1:1, at a GHSV in the range of from about 1250 hr, under a pressure in the range of from about 30 barg to about 42 barg, and at a temperature in the range of from about 160° C. to about 280° C.'}2. A process for improving performance of a Fischer-Tropsch catalyst comprising the steps of:{'sup': −1', '−1, '(a) contacting the catalyst with hydrogen or syngas at a temperature in the range of from about 200° C. to about 450° C., under a pressure in the range of from about 0 barg to about 50 ...

METHODS AND COMPOSITIONS FOR DIRECT, SIMULTANEOUS CONVERSION OF NITROGEN AND NATURAL GAS TO VALUE-ADDED COMPOUNDS

In one aspect, the disclosure relates to processes for production of ammonia and hydrogen under low reaction severity using as reactants nitrogen and at least one C1-C4 hydrocarbon, e.g., methane. The disclosed processes are carried out using a heterogeneous catalyst comprising a metal selected from Group 7, Group 8, Group 9, Group 10, Group 11, and combinations thereof; wherein the metal is present in an amount from about 0.1 wt % to about 20 wt % based on the total weight of the heterogeneous catalyst; and a metal oxide support. The processes can be carried out at about ambient pressure and at a heterogeneous catalyst temperature of from about 50° C. to about 250° C. This abstract is intended as a scanning tool for purposes of searching in the particular art and is not intended to be limiting of the present disclosure. 1. A process for synthesizing ammonia , comprising: wherein the heterogeneous catalyst comprises a metal selected from the group consisting of Group 7, Group 8, Group 9, Group 10, Group 11, and combinations thereof; wherein the metal is present in an amount from about 0.1 wt % to about 20 wt % based on the total weight of the heterogeneous catalyst; and a metal oxide support;', 'wherein the reaction chamber is a microwave-assisted reactor system operated under reaction pressure of about 2 torr to about 100 atm;, 'providing a reaction chamber with a heterogeneous catalyst;'}conveying a flow of a reactant gas mixture into the reaction chamber via an entry port; 'wherein the reactant gas mixture comprises nitrogen and at least one C1-C4 hydrocarbon;', 'wherein the reaction temperature is from 160-650° C.'}contacting the reactant gas mixture and the heterogeneous catalyst; 'wherein the product gas mixture comprises ammonia, C2-C4 hydrocarbons, aromatics and hydrogen; and', 'heating the heterogeneous catalyst using microwave energy, thereby providing a product gas mixture;'}conveying the product gas mixture from the reaction chamber via an exit port.2. ...

Methods and apparatuses for regenerating catalysts for hydrocarbon production

Methods and apparatuses are provided for producing hydrocarbons. A method includes contacting an aromatic rich feed stream including diolefins with a catalyst in the presence of hydrogen to react the diolefins with the hydrogen to produce mono-olefins. A deposit forms on the catalyst during reaction. The deposit is removed from the catalyst with a solvent, where the solvent includes about 50 mass percent or more aromatic compounds.

METHODS OF TREATING AND SULFIDING HYDROCONVERSION CATALYSTS

Methods of treating hydroconversion catalysts used for cracking of hydrocarbons are described. A method can include mixing an inactive hydroconversion catalyst with a solid hydrocarbon containing material having a melting point of 50° C. or greater. The inactive hydroconversion catalyst/solid hydrocarbon containing material mixture can be contacted with a gaseous stream that includes hydrogen (H) and a sulfur-containing compound under conditions sufficient to sulfide the catalyst and carbonize at least a portion of the hydrocarbon containing material on the sulfided catalyst to obtain a treated sulfided hydroconversion catalyst. 1. A method of treating a hydroconversion catalyst , the method comprising:(a) combining an inactive hydroconversion catalyst with a solid hydrocarbon containing material having a melting point of 50° C. or greater; and{'sub': '2', '(b) sulfiding the inactive hydroconversion catalyst by contacting the unsulfided hydroconversion catalyst/solid hydrocarbon containing material mixture with a gaseous stream comprising hydrogen (H) and a sulfur-containing compound at a temperature sufficient to sulfide the catalyst and carbonize at least a portion of the hydrocarbon containing material on the sulfided catalyst to obtain a treated sulfided hydroconversion catalyst.'}2. The method of claim 1 , wherein the catalyst in step (a) is at a temperature lower than the melting point of the solid hydrocarbon containing material at the time the catalyst is contacted with the solid hydrocarbon containing material.3. The method of claim 2 , further comprising heating the mixture to a temperature sufficient to melt the hydrocarbon containing material4. The method of claim 1 , wherein the catalyst in step (a) is at a temperature greater than the melting point of the solid hydrocarbon containing material at the time the catalyst is contacted with the solid hydrocarbon containing material5. The method of claim 2 , wherein the temperature difference between the ...

Activation of a self-activating hydroprocessing catalyst with steam

A self-activating hydroprocessing catalyst for treating heavy hydrocarbon feedstocks is further activated by contacting the self-activating catalyst with steam. The steam may be added to the heavy hydrocarbon feedstock prior to contacting with the self-activating catalyst or may be added to a reactor vessel containing the self-activating catalyst.

PROCESS FOR REJUVENATING HYDROTREATING CATALYST

The invention refers to a process for rejuvenating a hydrotreating catalyst comprising a group VIB hydrogenation metal and/or a group VIII hydrogenation metal, which comprises the steps of: (a) regenerating the catalyst by contacting said catalyst with an oxygen containing gas at a temperature from about 300° C. to 550° C., (b) impregnating the regenerated carbon-reduced catalyst with an impregnation solution which comprises a mixture of water and a combination of MoOand HPO, (c) aging the impregnated catalyst and (d) drying the aged catalyst. The invention also refers to the rejuvenated catalyst obtained and its use for hydro-treating hydrocarbon feedstocks. 1. A process for rejuvenating a hydrotreating catalyst comprising a group VIB hydrogenation metal and/or a group VIII hydrogenation metal , which comprises the steps of:a) regenerating the catalyst by contacting said catalyst with an oxygen containing gas at a temperature from about 300° C. to 550° C.,{'sub': 3', '3', '4, 'b) impregnating the regenerated catalyst with an impregnation solution which consists of a mixture water and a combination of MoOand HPO, excluding any other compounds,'}c) aging the impregnated catalyst for at least 2 hours at room temperature andd) drying the aged catalyst. wherein the impregnation of the catalyst with said impregnation solution in step b) leads to the rejuvination of said catalyst.2. The process according to claim 1 , wherein the temperature of the drying step d) is comprised from 80° C. to 200° C. and preferably is 120° C.3. The process according to claim 1 , wherein the content of carbon at the end of the regeneration step a) is inferior to 0.5 wt % based on the total weight of the catalyst.4. The process according to claim 1 , wherein the concentration of MoOis comprised from 0.10 mol of MoO/mol of hydrogenation metals to 1.0 mol of MoO/mol of hydrogenation metals based on the regenerated catalyst.5. The process according to claim 1 , wherein the concentration of HPOis ...

INTEGRATED C3-C4 HYDROCARBON DEHYDROGENATION PROCESS

An integrated process for producing C3-C4 olefins or di-olefins including: contacting a hydrocarbon feed and a catalyst feed in a fluidized dehydrogenation reactor under conditions such that a product mixture is formed and the catalyst is at least partially deactivated; transferring the product mixture and the catalyst from the reactor to a cyclonic separation system under conditions such that the product mixture is converted to form a new product mixture and is separated from the catalyst; transferring at least a portion of the catalyst to a regenerator vessel and heating it in order to combust the coke deposited thereon; subjecting the catalyst to a conditioning step to form an oxygen-containing, at least partially reactivated catalyst; and transferring the partially reactivated catalyst back to the fluidized dehydrogenation reactor. 1. An integrated process for producing C3-C4 olefins or C3-C4 di-olefins comprising the steps of:{'b': '1', 'claim-text': (i) a C3-C4 hydrocarbon feed and', '(ii) a catalyst feed comprising a catalyst;', 'under conditions such that a step (1)(a) product mixture, comprising a C3-C4 target olefin or di-olefin, hydrogen and unreacted C3-C4 hydrocarbon feed, is formed;, '() (a) contacting, in a fluidized dehydrogenation reactor,'} 'the catalyst has coke deposited thereon and is at least partially deactivated such that it forms an at least partially deactivated catalyst; and', 'and'}(b) transferring the step (1)(a) product mixture and the at least partially deactivated catalyst from the fluidized dehydrogenation reactor to a cyclonic separation system, andunder conditions such that the step (1)(a) product mixture is converted to form a step (1)(b) product mixture; andthereafter substantially separating the step (1)(b) product mixture and the at least partially deactivated catalyst from each other;(c) transferring at least a portion of the at least partially deactivated catalyst to a regenerator vessel and heating the at least partially ...

PROCESS FOR THE CATALYTIC PREPARATION OF HYDROGEN CYANIDE FROM METHANE AND AMMONIA

The invention relates to a catalyst material comprising a support, a first metal and a second metal on said support. The first and second metals are in the form of a chemical compound. The first metal is Fe, Co or Ni, and the second metal is selected from the group consisting of Sn, Zn and In. The invention also relates to a process for the preparation of hydrogen cyanide (HCN) from methane (CH) and ammonia (NH), wherein the methane and ammonia are contacted with a catalyst according to the invention. 1. A catalyst material comprising a support , a first metal and a second metal on said support , wherein said first and second metal are in the form of a chemical compound , where said first metal is Fe , Co or Ni , and where said second metal is selected from the group consisting of Sn , Zn and In.2. A catalyst material according to claim 1 , wherein the support comprises an alumina claim 1 , a spinel of alumina claim 1 , an oxide claim 1 , a carbide claim 1 , a nitride claim 1 , or a carbonitride.3. A catalyst material according to claim 1 , wherein the first and second metal form a ternary compound with carbon or nitrogen.4. A catalyst material according to claim 1 , wherein the first metal comprises Co.5. A catalyst according to claim 1 , wherein the first metal comprises Co and the second metal comprises Sn.6. A catalyst according to claim 1 , wherein the ratio of the weight percent of Fe claim 1 , Co or Ni to Sn claim 1 , Zn or In is between about 5:1 and 1:5.7. A catalyst according to claim 1 , wherein the ratio of the weight percent of Fe claim 1 , Co or Ni to Sn claim 1 , Zn or In is about 1:2.4.8. A catalyst according to claim 1 , wherein the support is a ferromagnetic support.9. A catalyst according to claim 8 , wherein the support comprises Co and wherein the second metal is coated onto the support.10. A process for the preparation of hydrogen cyanide (HCN) from methane (CH) and ammonia (NH) claim 1 , wherein the methane and ammonia are contacted with a ...

Method for restoring activity to a spent hydroprocessing catalyst, a spent hydroprocessing catalyst having restored catalytic activity, and a hydroprocessing process

A regenerated spent hydroprocessing catalyst treated with a chelating agent and having incorporated therein a polar additive.

REGENERATION OF OXIDATIVE DEHYDROGENATION CATALYST IN A REACTOR

Disclosed herein is a process for the regeneration of oxidative dehydrogenation (OXO-D) catalyst in an alternate or separate regeneration reactor by employing controlled steam: air and time/pressure/temperature conditions. The process avoids destruction of the catalyst, and wear/tear on an OXO-D reactor. The regenerated catalyst is an iron based oxide catalyst which can be zinc or zinc-free. The iron based oxide catalyst is regenerated in the regeneration reactor by feeding an air/steam stream over a set amount of time, preferably about 6 days to yield a regenerated OXO-D catalyst. The regenerated catalyst is activated and re-utilized to produce butadienes. 1. A process for regenerating an iron-based spent oxidative dehydrogenation catalyst in a fixed bed reactor , the process comprising:{'sub': '2', 'passing a stream containing steam and air in a controlled fashion, together with an oxygen-containing gaseous mixture having Oto HC ratio is in the range of 0.2-1, and the steam to HC ratio is in the range of 10-15 over a spent iron-based oxidative dehydrogenation catalyst containing carbonaceous compounds in the fixed bed reactor; wherein the steam to air ratio is less than 20 moles; and,'}heating the carbonaceous compounds deposited on the spent iron-based oxidative dehydrogenation catalyst at a pressure of 0-150 psig and a temperature less than 705° C., (1300° F.), wherein the temperature is maintained substantially constant for a period less than 144 hours (6 days) in the fixed bed reactor, and thereby regenerating the spent iron-based oxidative dehydrogenation catalyst in the fixed bed reactor.2. The process of wherein the Oto HC ratio is 0.55 and the steam to HC ratio is 12.3. The process of wherein the steam to air ratio is less than 10 moles.4. The process of wherein the temperature in the range of 340-650° C.5. The process of wherein the reaction temperature is raised by adjusting steam rate at no more than about 10 MT/hour.6. The process of claim 1 , wherein ...

METHOD, SYSTEM, AND DEVICE FOR REMOVING HYDROGEN PEROXIDE OR HYDRAZINE FROM A PROCESS GAS STREAM

Provided herein is a device for removing residual hydrogen peroxide or hydrazine from an effluent gas stream which includes a metal oxide scrubber material configured to react with residual process gases under increased temperatures. Also provided are systems and methods of using the same. 1. A method of decomposing hydrazine gas within an effluent gas stream comprising: (i) a body having an outer surface, an inner surface forming a lumen, an inlet port in fluid communication with the lumen, and an outlet port in fluid communication with the lumen;', '(ii) an inlet diffuser disposed within the lumen in close proximity to the inlet port;', '(iii) an outlet screen disposed within the lumen in close proximity to the outlet port;', '(iv) scrubber material disposed within the lumen between the inlet diffuser and the outlet screen, wherein the scrubber material is selected from the group consisting of manganese oxide, copper oxide, nickel oxide, iridium on aluminum oxide, or any combination thereof;', '(v) a heater disposed on the outer surface of the body, wherein the heater is configured to heat the body;, '(a) providing an effluent process gas stream comprising residual hydrazine in a device comprising(b) heating the device to about 80° C. to 500° C.; and(c) controlling flow of the effluent process gas stream such that substantially all the residual hydrazine is removed from the effluent process gas stream.2. The method of claim 1 , wherein the device is heated to about 100° C. to 150° C.3. The method of claim 1 , wherein the scrubber material in the device is at least 70% manganese oxide.4. The method of claim 1 , wherein the scrubber material in the device is at least 30% copper oxide.5. The method of claim 1 , wherein the residual hydrazine in the effluent process gas stream has a concentration of 5% or less.6. The method of claim 5 , wherein at least about 90%-99.5% of the hydrazine is removed from the effluent process gas stream.7. The method of claim 5 , wherein ...

PROCESS FOR THE PREPARATION OF HALOGENATED ALKENES BY DEHYDROHALOGENATION OF HALOGENATED ALKANES

The present invention provides a process for the preparation of a (hydro)(chloro)fluoroalkene by contacting a reagent stream comprising a hydrochlorofluoroalkane with a catalyst in a reactor to dehydrochlorinate at least a portion of the hydrochlorofluoroalkane to produce a product stream comprising the (hydro)(chloro)fluoroalkene and hydrogen chloride (HCl), wherein the catalyst is selected from the group consisting of metal oxide catalysts, metal halide catalysts, zero-valent metal catalysts, carbon-based catalysts and mixtures thereof, and wherein (i) the catalyst is chlorinated prior to contacting it with the reagent stream comprising the hydrochlorofluoroalkane; and/or (ii) the contacting step is carried out in the presence of a HCl co-feed. 120.-. (canceled)21. A process for the preparation of a (hydro)(chloro)fluoroalkene , the process comprising:contacting a reagent stream comprising a hydrochlorofluoroalkane with a catalyst in a reactor to dehydrochlorinate at least a portion of the hydrochlorofluoroalkane to produce a product stream comprising the (hydro)(chloro)fluoroalkene and hydrogen chloride (HCl), wherein the catalyst is selected from metal oxide catalysts, metal halide catalysts, zero-valent metal catalysts, carbon-based catalysts and mixtures thereof;{'sup': −1', '−1, 'chlorinating the catalyst by contacting the catalyst with a fluid stream comprising a chlorinating agent for about 1 to about 48 hours, wherein the chlorinating agent has a space velocity of from about 0.1 minto about 5 minprior to contacting the catalyst with the reagent stream comprising, the hydrochlorofluoroalkane; and/or'}carrying out the contacting step of the reagent stream comprising a hydrochlorofluoroalkane with the catalyst in the presence of at least 1 mol % HCl co-feed based on the combined amount of hydrochlorofluoroalkane and HCl fed to the reactor.22. A process according to claim 21 , wherein the chlorinating agent comprises hydrogen chloride (HCl) claim 21 , chlorine ...

Redox catalysts for the oxidative cracking of hydrocarbons, methods of making, and methods of use thereof

A variety of redox catalysts, methods of making, and methods of using thereof are provided. Surface modified redox catalysts are provided having an oxygen carrier core with an outer surface that has been modified to enhance the selectivity of the redox catalyst for oxidative dehydrogenation. The surface modification can include forming a redox catalyst outer layer on the outer surface and/or suppressing sites that form nonselective electrophilic oxygen sites on the outer surface of the oxygen carrier. A variety of methods are provided for making the surface modified redox catalysts, e.g. modified Pechini methods. A variety of methods are provided for using the catalysts for oxidative cracking of light paraffins. Methods are provided for oxidative cracking of light paraffins by contacting the paraffin with a core-shell redox catalyst described herein to convert the paraffins to water and olefins, diolefins, or a combination thereof.

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

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

PROCESS FOR THE TREATMENT OF REFINERY PURGE STREAMS

The present invention relates to a process for the treatment of refinery purge streams, containing a hydrocarbon component in slurry phase having a boiling point higher than or equal to 140° C., characterized by the presence of quantities of asphaltenes higher than or equal to 5% by weight and characterized by the presence of a solid content higher than or equal to 5% by weight. The process provides that said purge be mixed with a suitable fluxing agent according to appropriate ratios and under certain conditions, forming a suspension with a content higher than or equal to 10% by weight of compounds having a boiling point TbP lower than or equal to 350° C. After mixing, the suspension is sent to a liquid/solid separation step which operates under suitable conditions, separating a solid phase containing a residual organic component and a solid component, called cake, and a liquid phase containing residual solids. The solid phase obtained is cooled to below 60° C., including the upper extreme, forming a granular solid which is stored and maintained at a temperature lower than or equal to 60° C. 1. A process for the treatment of refinery purge streams , the process comprising:a) withdrawing a refinery purge stream comprising a hydrocarbon component in slurry phase having a boiling point higher than or equal to 140° C., characterized by the presence of quantities of asphaltenes higher than or equal to 5% by weight and characterized by the presence of solid contents greater than or equal to 5% by weight;{'sub': 'bp', 'b) mixing said purge, at a temperature higher than or equal to 100° C., with a mixture of hydrocarbons or fluxing agent, having a total content of aromatic compounds ranging from 50% to 70% by weight, and an initial boiling point equal to or higher than the temperature at which the mixing is carried out, so as to form a suspension with a content higher than or equal to 10% by weight of compounds having a boiling point Tlower than or equal to 350° C.;'}c) ...

CATALYTIC REACTION

Reaction methods are disclosed including induction catalysts. Such reactions may involve heating a catalyst by inductive heating; contacting the catalyst with a composition such that a reaction occurs and removing a reaction product. Example reactions include catalysts with ferrimagnetic metal oxide material and reactions involving organic reactants. 1. A low temperature method of polymerizing alcohol comprising:a. introducing an alcohol into a reactor;b. introducing iron oxide into the reactor;c. regulating a reactor temperature such that it reaches between 100° C. and 300° C. andd. maintaining the reactor temperature between 100° C. and 300° C. for a time period sufficient to polymerize the alcohol;e. wherein a first product of the polymerizing of the alcohol is a cyclic compound andf. wherein the first product of the polymerizing of the alcohol exhibits fluorescence.2. The method of wherein the alcohol is butanol.3. The method of wherein the alcohol is selected from butanol claim 1 , pentanol and hexanol.4. The method of wherein the maintaining of the reactor temperature is between 150 and 250° C.5. The method of wherein radio-frequency heating is used in the maintaining of the reactor temperature.6. The method of wherein the iron oxide is FeOnanoparticles.7. The method of wherein the iron oxide is FeOparticles that are less than 10 micrometers.8. The method of wherein the maintaining the reactor temperature between 100° C. and 300° C. occurs for at least 4 hours.9. The method of wherein the polymerizing of the alcohol occurs as a batch processing reaction.10. The method of wherein a majority of the iron oxide is spherical particles.11. The method of wherein a majority of the iron oxide is cube particles.12. The method of wherein a majority of the iron oxide is FeOnanoparticles.13. The method of wherein the first product is a heterocyclic compound.14. The method of wherein the first product contains a five-member ring structure.15. The method of wherein the first ...

Process for Selective Removal of Acetylenes from Gaseous Streams

The present discloses a process and catalyst therefor to selectively remove acetylenes from gaseous streams in the vapor phase. The process is particularly suitable for high yield recovery of olefinic hydrocarbons from gaseous streams in refinery processes.

METHOD FOR REGENERATING CATALYST FOR BUTADIENE PRODUCTION

An object of the present invention is to provide a method for regenerating a catalyst for butadiene production, for removing a coke-like substance which is generated by oxidative dehydrogenation of n-butene in the presence of a catalyst for butadiene production and which is attached to the catalyst and the inside of a reactor. After the catalyst is used in oxidative dehydrogenation of butenes, the catalyst regeneration method of the present invention removes a coke-like substance in a reactor which is charged with the catalyst for butadiene production, the catalyst having a prescribed composition before being used in the oxidative dehydrogenation. 2. The catalyst regeneration method according to claim 1 ,{'sub': 2', '2, 'wherein the gas supplying is conducted after a generation speed of COand CO discharged from the reactor has reached a maximum generation speed during the gas treatment conducted under a condition defined above, when the generation speed of COand CO discharged from the reactor decreases to 95% or less of the maximum generation speed.'}3. The catalyst regeneration method according to claim 2 ,wherein a cycle comprising the gas treatment and the subsequent gas supplying is repeated twice or more, andwherein a temperature of the heat medium during the gas treatment and the gas supplying in a first cycle and a temperature of the heat medium during the gas treatment and the gas supplying in a second cycle are different.4. The catalyst regeneration method according to claim 3 ,wherein the temperature of the heat medium during the gas treatment and the gas supplying in the second cycle is higher than the temperature of the heat medium during the gas treatment and the gas supplying in the first cycle.5. The catalyst regeneration method according to claim 1 ,wherein the temperature of the heat medium circulating in the reactor is between not less than 200° C. and not greater than 350° C.6. The catalyst regeneration method according to claim 1 ,wherein the ...

Method, system, and device for removing hydrogen peroxide or hydrazine from a process gas stream

Provided herein is a device for removing residual hydrogen peroxide or hydrazine from an effluent gas stream which includes a metal oxide scrubber material configured to react with residual process gases under increased temperatures. Also provided are systems and methods of using the same.

CATALYTIC GAS PHASE FLUORINATION

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

MIXED-CONDUCTOR ENHANCED COMPOSITE AND CORE-SHELL OXIDES FOR CYCLIC REDOX PRODUCTION OF FUELS AND CHEMICALS

Compositions and methods for preparing and using ceramic mixed ionic-electronic conductor (MIEC) enhanced transition metals and metal oxides in composite or core-shell forms are disclosed. The presently disclosed compositions are stable at high temperatures and can carry as much as about 20 weight % oxygen. 1. A redox catalyst comprising an oxygen carrying material , a mixed ionic-electronic conductive (MIEC) support , and a catalytically-active surface.2. The redox catalyst of claim 1 , wherein the oxygen carrying material comprises a metal oxide.3. The redox catalyst of claim 2 , wherein the metal oxide comprises a transition metal oxide and mixtures thereof.4. The redox catalyst of claim 3 , wherein the transition metal oxide comprises an oxide of a transition metal selected from the group consisting of Mn claim 3 , Fe claim 3 , Co claim 3 , Ni claim 3 , V claim 3 , Mo claim 3 , Cu claim 3 , Zn claim 3 , S and mixtures thereof.5. The redox catalyst of claim 2 , wherein the metal oxide comprises a spinel oxide having a formula ABO claim 2 , wherein A and B are each independently a metal cation or a combination of metal cations.6. The redox catalyst of claim 5 , wherein the metal cation is selected from the group consisting of magnesium claim 5 , calcium claim 5 , strontium claim 5 , barium claim 5 , zinc claim 5 , iron claim 5 , manganese claim 5 , aluminum claim 5 , chromium claim 5 , titanium claim 5 , and silicon.7. The redox catalyst of claim 1 , wherein the MIEC support has a perovskite structure.8. The redox catalyst of claim 1 , wherein the MIEC support is selected from the group consisting of LaSrFeO claim 1 , BaCeFeO claim 1 , and CaTiFeO claim 1 , wherein 0.2 Подробнее

REGENERATION OF CATALYST FOR HYDROGENATION OF SUGARS

A process for regenerating catalysts that have been deactivated or poisoned during hydrogenation of biomass, sugars and polysaccharides is described, in which polymerized species that have agglomerated to catalyst surfaces can be removed by means of washing the catalyst with hot water at subcritical temperatures. A feature of the process can regenerate the catalysts in situ, which allows the process to be adapted for used in continuous throughput reactor systems. Also described is a continuous hydrogenation process that incorporated the present regeneration process. 1. A method of regenerating hydrogenation catalyst activity in-situ , the method comprising: a) providing a hydrogenation reactor , said reactor being configured to have at least a first and a second vessel , said first vessel having a first catalyst and said second vessel having a second catalyst , said first and second catalysts being either the same or of a different material; and b) rinsing each respective vessel and catalyst with subcritical deionized water of between about 130° C.-250° C. for an extended period.2. The method according to claim wherein said method further comprises: introducing a subcritical deionized aqueous solution containing HOin a concentration of ≦7% by volume to said first catalyst in said first vessel of said reactor when catalytic activity of said first catalyst decreases to a predetermined level; or introducing periodically an aqueous salt solution to either 1) said first catalyst in first vessel or 2) said second catalyst when catalytic activity of said second catalyst decreases to a predetermined level; removing respectively said aqueous HOsolution from said first vessel and said aqueous salt solution from said first or second vessels of said reactor.3. The method according to claim 1 , wherein said first and second vessels are arranged either in serial communication or in parallel communication with each other.4. The method according to claim 1 , wherein said first or ...

Olefin production method using circulating fluidized bed process

Disclosed is an olefin production method which includes: (a) providing the regenerated catalyst and the hydrocarbon including not less than 90 wt % of LPG into Riser of Fast Fluidization Regime, and dehydrogenating in the presence of an alumina type catalyst; (b) separating an effluent from the dehydrogenation reaction into the catalyst and propylene mixture; (c) stripping to remove the hydrocarbon compound included in the catalyst separated at stage (b); (d) mixing the catalyst stripped at stage (c) with the gas including oxygen, and continuously regenerating it; (e) recycling the catalyst regenerated at stage (d) to stage (a), and providing it again into Riser; and (f) producing propylene product by cooling, compressing and separating propylene mixture of the reaction product separated at stage (b).

REGENERATION OF CATALYST FOR HYDROGENATION OF SUGARS

A process for regenerating catalysts that have been deactivated or poisoned during hydrogenation of biomass, sugars and polysaccharides is described, in which polymerized species that have agglomerated to catalyst surfaces can be removed by means of washing the catalyst with hot water at subcritical temperatures. A feature of the process can regenerate the catalysts in situ, which allows the process to be adapted for used in continuous throughput reactor systems. Also described is a continuous hydrogenation process that incorporated the present regeneration process. 1. A method of regenerating hydrogenation catalyst activity in-situ , the method comprising: a) providing a hydrogenation reactor , said reactor being configured to have a first and a second vessel , said first vessel having a first catalyst and said second vessel having a second catalyst , said first and second catalysts being either the same or a different material; and b) rinsing each respective vessel and catalyst with subcritical deionized water of between about 130° C.-250° C. for an extended period.2. The method according to claim 1 , wherein said method further comprises: introducing a subcritical deionized aqueous solution containing HOin a concentration of ≦7% by volume to said first catalyst in said first vessel of said reactor when catalytic activity of said first catalyst decreases to a predetermined level; or introducing periodically an aqueous salt solution to either 1) said first catalyst in first vessel or 2) said second catalyst when catalytic activity of said second catalyst decreases to a predetermined level; removing respectively said aqueous HOsolution from said first vessel and said aqueous salt solution from said first or second vessels of said reactor.3. The method according to claim 1 , wherein said first and second vessels are arranged either in serial communication or in parallel communication with each other.4. The method according to claim 1 , wherein said first or second ...

PROCESSES AND APPARATUS FOR INTRODUCING A GAS INTO A REACTOR

A method for producing a dehydrogenated product and a coked catalyst, then introducing an oxygen-containing fluid, combusting at least a portion of the coke disposed on the catalyst in the presence of the oxygen-containing fluid to produce a decoked catalyst. An apparatus for introducing fluid into a reactor, comprising a first inlet conduit configured to convey a first gas, a second inlet conduit configured to convey a second gas, and an outlet conduit configured to convey the first gas and the second gas into a reactor, wherein there is an acute angle between a longitudinal axes of the first inlet conduit and a longitudinal axis of the second inlet conduit and an obtuse angle between a longitudinal axis of the outlet conduit and the longitudinal axis of the second inlet conduit and a pre-distributor disposed, in one embodiment on the inner surface, within the first inlet conduit is disclosed. 1. An inlet assembly for introducing a fluid into a reactor , comprising:a first inlet conduit, a second inlet conduit, and an outlet conduit fluidly connected at a junction, wherein the first inlet conduit is configured to convey a first gas therethrough, the second inlet conduit is configured to convey a second gas therethrough, and the outlet conduit is configured to convey the first gas and the second gas therethrough and into a reactor, wherein there is an acute angle between a longitudinal axes of the first inlet conduit and a longitudinal axis of the second inlet conduit and an obtuse angle between a longitudinal axis of the outlet conduit and the longitudinal axis of the second inlet conduit; anda pre-distributor disposed within the first inlet conduit.2. The inlet assembly of claim 1 , wherein a cross-sectional area of the first inlet conduit at the junction is greater than a cross-sectional area of the second inlet conduit at the junction.3. The inlet assembly of claim 1 , further comprising a third inlet conduit fluidly connected to the junction and configured to ...

OLIGOMERIZATION OF ETHENE IN SUPERCRITICAL MODE

The invention is concerned with the oligomerization of supercritical ethene. An essential aspect of the invention is that of mixing ethene with an inert medium and setting the conditions in the reaction such that both ethene and inert medium are supercritical. This is because the solubility for ethene in the inert medium is greater in the supercritical state, such that more ethene is dissolved in the supercritical inert medium than in a liquid solvent. The process regime in the supercritical state therefore enables the use of a much higher proportion of ethene in a homogeneous mixture of ethene and inert medium than is possible on the basis of the thermodynamic solubility restriction in a purely liquid hydrocarbon stream. In this way, the space-time yield is distinctly enhanced. Since a greater amount of ethene can be passed into the reactor, it is possible as a result to better exploit the apparatus volume compared to a liquid phase process. The inert medium used may, for example, be isobutane. 1. A process for oligomerizing ethene , in which a mixture comprising ethene and an inert medium contacts a solid catalyst , characterized in that the proportion by weight of the inert medium in the mixture is greater than the proportion by weight of ethene in the mixture , the inert medium is an alkane or a cycloalkane , where the alkane or cycloalkane has not less than three and not more than seven carbon atoms , and pressure and temperature of the mixture are chosen with respect to the proportion of ethene in the mixture such that ethene and inert medium are in the supercritical state.2. The process according to claim 1 , wherein the mixture is at first provided in the supercritical state and then contacted with the solid catalyst claim 1 , where the provision of the mixture in the supercritical state is affected either according to alternative a) or according to alternative b):a) inert medium is converted to the supercritical state by increasing the pressure and/or ...

CHANNEL REACTORS

Described is an industrial scale chemical reactor or reactor containing a shell having an inner wall, and at least one channel inside the shell. The shell has a circular, square, or rectangular cross-sectional area. All of the internal dimensions of the channel are greater than 10 mm, and optionally less than 50 mm. The channel has a rectangular cross-sectional area, and contains a catalyst bed containing catalyst particles and/or pieces containing catalyst particles packed inside the channel. The reactor has improved shell volume utilization, catalyst loading capacities, heat exchange efficiency, process intensification, or combinations thereof, compared to currently existing reactors. Exothermic reactions, such as the Fischer-Tropsch synthesis can be performed inside the channels of the reactor. Also described are methods of making the reactor. 1. An industrial scale chemical reactor comprising:a shell defined by one or more walls, wherein each wall comprises an inner surface;a rectangular channel inside the shell, wherein each internal dimension of the channel is greater than 10 mm;a catalyst bed inside the channel, wherein catalyst particles or pieces containing catalyst particles are packed in the bed; anda gap between the channel and the inner surface of the wall.2. The reactor of claim 1 , wherein the shell has a circular or square cross-section.3. The reactor of claim 1 , wherein the total volume of the channel is more than 50% of the shell volume.4. The reactor of claim 1 , comprising two or more rectangular channels claim 1 , and wherein the channels are aligned in the same direction.5. The reactor of claim 1 , wherein the channel is formed from a metal claim 1 , metal alloy claim 1 , or ceramic with a thermal conductivity between 10 W/m·K and 4000 W/m·K claim 1 , inclusive.6. The reactor of claim 1 , comprising two or more rectangular channels claim 1 , and further comprising a second gap between adjacent channels.7. The reactor of claim 1 , wherein the ...

METHODS FOR CONVERSION OF METHANE TO SYNGAS

Methods and systems for converting methane to syngas are provided. Certain exemplary methods and systems involve reacting methane and carbon dioxide with a nickel oxide catalyst in a reaction chamber, thereby providing syngas and a reduced nickel species. The reduced nickel species can be regenerated by oxidation with air in a regeneration chamber, thereby generating a regenerated nickel oxide and heat. The regenerated nickel oxide and heat can be returned to the reaction chamber to drive the syngas reaction. 1. A method for preparing syngas , comprising:a. providing a reaction chamber and a regeneration chamber, wherein the reaction chamber comprises a nickel oxide;b. feeding methane and carbon dioxide to the reaction chamber, thereby contacting methane and carbon dioxide with the nickel oxide to provide syngas and a reduced nickel species;c. removing the reduced nickel species from the reaction chamber to the regeneration chamber;d. feeding air to the regeneration chamber, thereby contacting air with the reduced nickel species to provide a regenerated nickel oxide and heat; ande. removing the regenerated nickel oxide and heat from the regeneration chamber to the reaction chamber.2. The method of claim 1 , wherein the nickel oxide comprises a solid support.3. The method of claim 2 , wherein the solid support comprises an oxide selected from the group consisting of aluminum oxide claim 2 , magnesium oxide claim 2 , and silicon oxide.4. The method of claim 1 , wherein the nickel oxide comprises particles having a diameter between about 200 μm and about 400 μm.5. The method of claim 1 , wherein the nickel oxide comprises a promoter.6. The method of claim 5 , wherein the promoter comprises an oxide selected from the group consisting of lanthanum(III) oxide claim 5 , cerium(III) oxide claim 5 , platinum(II) oxide claim 5 , barium oxide claim 5 , calcium oxide claim 5 , and potassium oxide.7. The method of claim 1 , wherein the temperature in the reaction chamber is ...

METHOD OF COUPLING METHANE DRY-REFORMING AND COMPOSITE CATALYST REGENERATION

The present invention is related to a method of coupling methane dry-reforming and composite catalyst regeneration. A composite catalyst is filled into a reactor, and methane or a methane mixture gas is introduced therein. CaCOin the composite catalyst is decomposed under 600-850° C. COobtained by the decomposition reacts with methane to perform methane dry-reforming reaction and produce synthesis gas containing CO and hydrogen. The composite catalyst contains CaCO, active nickel and alumina support. This method couples the CaCOdecomposition reaction in calcium looping and methane dry-reforming reaction to solve the technical problem of limiting CaCOdecomposition by high-temperature equilibrium. The decomposition of CaCOis enhanced, and the COproduced by decomposing CaCOis dry-reformed to produce synthesis gas to be utilized. 110-. (canceled)11. A method of coupling methane dry-reforming and composite catalyst regeneration , comprising:{'sub': 3', '2', '3, 'filling a first composite catalyst into a reactor, wherein the first composite catalyst comprises CaCOand an active nickel containing NiO supported on a support containing alumina (AlO);'}introducing a methane-containing gas into the reactor;{'sub': 3', '2, 'decomposing the CaCOin the first composite catalyst at 600-850° C. to obtain COand CaO; and'}{'sub': 2', '2, 'performing methane dry reforming reaction by reacting the obtained COwith methane in the methane-containing gas to form synthesis gas containing CO and H.'}12. The method of claim 11 , wherein a mass ratio of CaO claim 11 , NiO and AlOin the first composite catalyst is 2-7:1:1.0-3.5.13. The method of claim 11 , wherein the methane-containing gas is methane claim 11 , or a mixture of methane and at least one of water vapor claim 11 , COand nitrogen.14. The method of claim 11 , wherein a volume ratio of the methane in the methane-containing gas is at least 10%.15. The method of claim 11 , wherein the decomposing step is performed under a pressure of 0.1 ...

Reactivated Hydroprocessing Catalysts for Use in Sulfur Abatement

Disclosed herein are methods, systems, and compositions for providing catalysts for tail gas clean up in sulfur recovery operations. Aspects of the disclosure involve obtaining catalyst that was used in a first process, which is not a tailgas treating process and then using the so-obtained catalyst in a tailgas treating process. For example, the catalyst may originally be a hydroprocessing catalyst. A beneficial aspect of the disclosed methods and systems is that the re-use of spent hydroprocessing catalyst reduces hazardous waste generation by operators from spent catalyst disposal. Ultimately, this helps reduce the environmental impact of the catalyst life cycle. The disclosed methods and systems also provide an economically attractive source of high-performance catalyst for tailgas treatment, which benefits the spent catalyst generator, the catalyst provider, and the catalyst consumer.

REGENERATION OF CATALYST

A catalyst is regenerated by an inventive process using a heat exchange fluid such as superheated steam to remove heat during the process relying on efficient heat transfer (e.g., enabled by the microchannel reactor construction) in comparison with prior art heat exchange relying on a phase change, e.g. between water and (partial or complete vaporization) steam, allows simplification of the protocols to enable transition at higher temperatures between steps which translates in reduced duration of the regeneration process and avoids potential water hammering risks. 1. A process for regeneration of a catalyst iii 11 in a reactor , preferably a microchannel reactor , provided with heat exchange channels , the process comprising:a) de-waxing the catalyst by treating it at an elevated temperature with a hydrogen containing de-waxing gas stream flowing through process microchannels of the reactor;b) oxidising the resulting de-waxed catalyst by treating it at an elevated temperature with an oxidising gas stream flowing through process microchannels of the reactor, andc) reducing the resulting oxidised catalyst by treating it at an elevated temperature with a reducing gas stream flowing through process microchannels of the reactor,wherein:in the transition from step a) to step b) the temperature inside the process microchannels and/or the heat exchange channels is lowered from a temperature sufficient for de-waxing to a first lower limit value of 90° C. or greater, preferably 100° C. or greater, more preferably 140° C. to 180° C., most preferably 145° C. to 155° C.;in step b) the temperature inside the process microchannels and/or the heat exchange channels is raised to a temperature sufficient to oxidise the catalyst;in the transition from step b) to step c) the temperature inside the process microchannels and/or the heat exchange channels is lowered from a temperature sufficient for oxidation to a first lower limit value of 90° C. or greater, preferably 100° C. or greater ...

Procede pour limiter les emissions de gaz a partir de particules poreuses

La présente invention a pour objet un procédé pour limiter les émissions de gaz à partir d'un matériau poreux sous forme de particules. Les particules sont placées en mouvement au sein d'un flux de gaz chaud les traversant, et une composition liquide contenant un ou plusieurs polymère(s) filmogène(s) est pulvérisée sur les particules en mouvement au moyen d'une buse d'atomisation bi-fluide dans laquelle la composition liquide est mélangée avec un gaz sous pression, avec une pression relative d'atomisation supérieure ou égale à 0,7. 105 Pa, jusqu'à l'obtention sur la surface desdites particules d'une couche protectrice contenant le (les) polymère(s) filmogène(s) et présentant une épaisseur moyenne inférieure ou égale à 20 µm. La présente invention a également pour objet un matériau sous forme de particules recouvertes d'une couche protectrice, susceptible d'être obtenu par ce procédé.

METHOD FOR IMPROVING A CATALYST

Process for regenerating a catalyst

A PROCESS FOR REGENERATING A FIXED BED OF FISCHER- TROPSCH CATALYST PARTICLES, OF WHICH AT LEAST 40 WT% OF THE CATALYST PARTICLES HAS A SIZE OF AT LEAST 1MM, IN SITUIN A FISCHER-TROPSCH REACTOR TUBE. THE PROCESS COMPRISES THE STEPS OF: (I) OPTIONALLY OXIDISING THE CATALYST AT A TEMPERATURE BETWEEN 200 AND 400 °C; (II) OXIDISING THE CATALYST AT A TEMPERATURE ABOVE 580°C AND BELOW 670 °C; AND (III) REDUCING THE CATALYST WITH HYDROGEN OR A HYDROGEN COMPRISING GAS. THIS PROCESS MAY BE PRECEDED BY A STEP IN WHICH FISCHER-TROPSCH PRODUCT IS REMOVED FROM THE CATALYST.

Regenerating copper-containing catalysts used in hydrogenation of methylol-aldehydes to methylol-alcohols involves treatment in oxygen-containing medium and re-activation in hydrogen-containing medium

Catalysts containing copper as an active component ,and used in the hydrogenation of methylol-aldehydes to methylol-alcohols, are regenerated in an oxygen-containing medium and activated prior to re-use in a hydrogen-containing medium. An Independent claim is included for use of the catalyst regeneration process is in the hydrogenation of hydroxypivalaldehyde, 2,2-dimethylolbutanal, 2,2-dimethylolpropionaldehyde, 3-hydroxypropionaldehyde and/or trimethylolacetaldehyde.

Process for limiting the emissions of gases from porous particles

A process is disclosed for limiting the emissions of gases from a porous material in the form of particles comprising a porous inorganic support and at least 0.1% by weight of one or more compounds chosen from organic compounds, halogen compounds, boron compounds and phosphorus compounds. The particles are placed in motion within a hot gas stream traversing them, and a liquid composition containing one or more film-forming polymer(s) is sprayed over the moving particles by means of a twin-fluid atomization nozzle, in which the liquid composition is mixed with a pressurized gas, with a relative atomization pressure of greater than or equal to 0.7×1005 Pa, until a protective layer containing the film-forming polymer(s) and exhibiting a mean thickness of less than or equal to 20 μm is obtained on the surface of the said particles. A material resulting from this process is also disclosed.

METHOD FOR LIMITING GAS EMISSIONS FROM POROUS PARTICLES

La présente invention a pour objet un procédé pour limiter les émissions de gaz à partir d'un matériau poreux sous forme de particules. Les particules sont placées en mouvement au sein d'un flux de gaz chaud les traversant, et une composition liquide contenant un ou plusieurs polymère(s) filmogène(s) est pulvérisée sur les particules en mouvement au moyen d'une buse d'atomisation bi-fluide dans laquelle la composition liquide est mélangée avec un gaz sous pression, avec une pression relative d'atomisation supérieure ou égale à 0,7. 105 Pa, jusqu'à l'obtention sur la surface desdites particules d'une couche protectrice contenant le (les) polymère(s) filmogène(s) et présentant une épaisseur moyenne inférieure ou égale à 20 µm. La présente invention a également pour objet un matériau sous forme de particules recouvertes d'une couche protectrice, susceptible d'être obtenu par ce procédé. The present invention relates to a method for limiting gas emissions from a porous material in the form of particles. The particles are placed in motion within a flow of hot gas therethrough, and a liquid composition containing one or more film-forming polymer (s) is sprayed onto the moving particles by means of an atomizing nozzle. bi-fluid in which the liquid composition is mixed with a gas under pressure, with a relative atomization pressure greater than or equal to 0.7. 105 Pa, until the surface of said particles is obtained with a protective layer containing the film-forming polymer (s) and having an average thickness less than or equal to 20 μm. The present invention also relates to a material in the form of particles coated with a protective layer, obtainable by this method.

processo para eliminar as emissões de gases

PROCESSO PARA LIMITAR AS EMISSÕES DE GASES E MATERIAL POROSO. A presente invenção a por objeto um processo para limitar as emissões de gases a partir de um material poroso em forma de partículas que compreendem um suporte inorgânico poroso e pelo menos 0,1% em peso de um ou mais compostos escolhido entre os compostos orgânicos, os compostos halogenados, os compostos borados e os compostos fosforados. As partículas são postas em movimento no interior de um fluxo de gás quente que as atravessam, e uma composição líquida que contém um ou mais polímero(s) filmogênio(s) é pulverizada sobre as partículas em movimento por meio de uma bico de atomização bi-fluido no qual a composição líquida é misturada com um gás sob pressão, com uma pressão relativa de atomização superior ou igual a 0,7.105 Pa, até a obtenção sobre a superfície das referidas partículas de uma camada protetora que contém o (os) polímero(s) filmogênio(s) e que apresenta uma espessura média inferior ou igual a 20 μm. A presente invenção possui igualmente por objeto um material em forma de partículas recobertas de uma camada protetora, suscetível de ser obtido esse processo.

Способ уменьшения выделений газа из пористых частиц

Объектом настоящего изобретения является способ уменьшения выделений газов из пористого материала в виде частиц, содержащих неорганическую пористую основу и в суммарном содержании по меньшей мере 0,1 вес.% от общего веса указанных частиц одного или нескольких соединений, выбранных из органических соединений, галогенированных соединений, борсодержащих соединений и фосфорсодержащих соединений. Частицы приводят в движение в потоке проходящего через них горячего газа, и на движущиеся частицы распыляют жидкую композицию, содержащую один или несколько пленкообразующих полимеров, с помощью двухкомпонентной распылительной форсунки, в которой жидкая композиция смешивается с газом под давлением, при относительном давлении распыления, которое соответствует разнице давлений между давлением газа внутри форсунки и атмосферным давлением больше или равном 0,7⋅10 5 Па до получения на поверхности указанных частиц защитного слоя, содержащего указанные один или несколько пленкообразующих полимеров и имеющего среднюю толщину меньше или равную 20 мкм. Объектом настоящего изобретения является также материал в виде пористых частиц для использования в качестве катализатора или адсорбента, покрытых защитным слоем, который может быть получен этим способом. Причем указанный пленкообразующий полимер или полимеры составляют от 0,1 до 4 вес.% от общего веса частиц и выбраны из: гомо- и сополимеров винилового спирта; полиэтиленгликолей; коллагена; полиэтилентерефталатов; полиэтиленнафталатов; полиамидов; полисахаридов; поливинилхлоридов; поливинилиденхлоридов; полиакрилонитрилов; полиакрилатных смол; сополимеров, в которых по меньшей мере один из мономеров является мономером акрилатного типа; и их смесей. Технический результат - снижение потенциального выделения газа из пористых материалов в виде частиц, содержащих органические соединения, галогенированные соединения, борсодержащие соединения и/или фосфорсодержащие соединения. 2 н. и 17 з.п. ф-лы, 2 табл., 9 пр. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) ( ...

PROCEDURE TO PREVENT GAS EMISSION FROM POROUS PARTICULARS

Method for supressing gas emissions out of porous particles

用于限制多孔粒子散发气体的方法

本发明的主题是一种用于限制粒子形式的多孔材料散发气体的方法，所述多孔材料包含多孔无机载体和至少0.1重量％的选自有机化合物、卤素化合物、硼化合物和磷化合物的一种或多种化合物。所述粒子在穿过所述粒子的热气流中处于运动状态，并且含有一种或多种成膜聚合物的液体组合物通过双流体雾化喷嘴以大于或等于0.7×10 5 Pa的相对雾化压力喷射在运动中的粒子上，直到在所述粒子的表面上获得含有所述成膜聚合物并且显示出小于或等于20μm的平均厚度的保护层，其中所述液体组合物与加压气体混合。本发明的另一个主题是覆盖有保护层的粒子形式的材料，该材料能够通过这一方法获得。

How to limit outgassing from porous particles

PROCESS FOR REGENERATING HYDROCARBON PROCESSING CATALYSTS

用于限制多孔粒子散发气体的方法

本发明的主题是一种用于限制粒子形式的多孔材料散发气体的方法，所述多孔材料包含多孔无机载体和至少0.1重量％的选自有机化合物、卤素化合物、硼化合物和磷化合物的一种或多种化合物。所述粒子在穿过所述粒子的热气流中处于运动状态，并且含有一种或多种成膜聚合物的液体组合物通过双流体雾化喷嘴以大于或等于0.7×10 5 Pa的相对雾化压力喷射在运动中的粒子上，直到在所述粒子的表面上获得含有所述成膜聚合物并且显示出小于或等于20μm的平均厚度的保护层，其中所述液体组合物与加压气体混合。本发明的另一个主题是覆盖有保护层的粒子形式的材料，该材料能够通过这一方法获得。

Method for reducing gas emissions by means of porous particles

La présente invention a pour objet un procédé pour limiter les émissions de gaz à partir d'un matériau poreux sous forme de particules comprenant un support inorganique poreux et au moins 0,1% en poids d'un ou plusieurs composés choisi parmi les composés organiques, les composés halogénés, les composés borés et les composés phosphorés. Les particules sont placées en mouvement au sein d'un flux de gaz chaud les traversant, et une composition liquide contenant un ou plusieurs polymère(s) filmogène(s) est pulvérisée sur les particules en mouvement au moyen d'une buse d'atomisation bi-fluide dans laquelle la composition liquide est mélangée avec un gaz sous pression, avec une pression relative d'atomisation supérieure ou égale à 0,7.10 5 Pa, jusqu'à l'obtention sur la surface desdites particules d'une couche protectrice contenant le (les) polymère(s) filmogène(s) et présentant une épaisseur moyenne inférieure ou égale à 20 µm. La présente invention a également pour objet un matériau sous forme de particules recouvertes d'une couche protectrice, susceptible d'être obtenu par ce procédé. The present invention relates to a method for limiting the gas emissions from a porous material in the form of particles comprising a porous inorganic support and at least 0.1% by weight of one or more compounds chosen from organic compounds. , halogenated compounds, boron compounds and phosphorus compounds. The particles are placed in motion within a flow of hot gas therethrough, and a liquid composition containing one or more film-forming polymer (s) is sprayed onto the moving particles by means of an atomizing nozzle. bi-fluid in which the liquid composition is mixed with a gas under pressure, with a relative atomization pressure of greater than or equal to 0.7 × 10 5 Pa, until a protective layer is obtained on the surface of said particles; the polymer (s) film-forming (s) and having an average thickness less than or equal to 20 microns. The ...

Patent RU2016151389A3

ВИ“? 2016151389” АЗ Дата публикации: 20.04.2020 Форма № 18 ИЗИМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение 5 «Федеральный институт промышленной собственности» (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2016151389/04(082432) 27.12.2016 Приоритет установлен по дате: [ ] подачи заявки [ ] поступления дополнительных материалов от к ранее поданной заявке № [ ] приоритета по первоначальной заявке № из которой данная заявка выделена [ ] подачи первоначальной заявки № из которой данная заявка выделена [ ] подачи ранее поданной заявки № [Х] подачи первой(ых) заявки(ок) в государстве-участнике Парижской конвенции (31) Номер первой(ых) заявки(ок) (32) Дата подачи первой(ых) заявки(ок) (33) Код страны 1. 15 63367 28.12.2015 ЕК Название изобретения (полезной модели): [Х] - как заявлено; [ ] - угочненное (см. Примечания) Способ уменьшения выделений газа из пористых частиц Заявитель: ЭРЕКА С.А, ЕК 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. Примечания) [ ] приняты во внимание следующие пункты: [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) ВО1. 33/00 (2006.01) ВО1.] 20/32 (2006.01) В05О 5/00 (2006.01) ВОЗВ 15/00 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) ВО11 33/00 (2006.0Т)Т ВО11 20/32 (2006.0Т)Т В05Р 5/00 (2006.0ОТ)УГ ВО8В 15/00 (2006.0101 5.2 Другая проверенная документация в той мере, в какой она включена в поисковые подборки: 5.3 Электронные базы данных, использованные при поиске (название базы, и если, возможно, поисковые термины): РУ/РТ, ЕАРАТГУ, Е5расепе, Соозе, Соозе Ра{еп($, Рабеагсв, КОРТО, За1епсе Оесь ОРТО 6. ДОКУМЕНТЫ, ОТНОСЯЩИЕСЯ К ПРЕДМЕТУ ПОИСКА Кате- Наименование документа с ...

Способ уменьшения выделений газа из пористых частиц

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2016 151 389 A (51) МПК B01J 23/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2016151389, 27.12.2016 (71) Заявитель(и): ЭРЕКА С.А (FR) Приоритет(ы): (30) Конвенционный приоритет: 28.12.2015 FR 15 63367 Адрес для переписки: 129090, Москва, ул. Б.Спасская, 25, строение 3, ООО "Юридическая фирма Городисский и Партнеры" A 2 0 1 6 1 5 1 3 8 9 давлением, при относительном давлении распыления больше или равном 0,7·105 Па, до получения на поверхности указанных частиц защитного слоя, содержащего указанные один или несколько пленкообразующих полимеров и имеющего среднюю толщину меньше или равную 20 мкм. 2. Способ по предыдущему пункту, отличающийся тем, что относительное давление распыления составляет от 0,7·105 до 4·105 Па, более предпочтительно от 1,2·105 до 3·105 Па, еще более предпочтительно от 1,5·105 до 2,5·105 Па и еще лучше от 1,7·105 до 2,3·105 Па. 3. Способ по одному из предыдущих пунктов, отличающийся тем, что жидкая композиция представляет собой раствор или дисперсию пленкообразующего полимера или полимеров в растворителе и предпочтительно содержит от 0,1 до 50 вес.% пленкообразующего полимера, более предпочтительно от 0,5 до 25 вес.% и еще более предпочтительно от 1 до 10 вес.% пленкообразующего полимера, от полного веса композиции. 4. Способ по одному из предыдущих пунктов, отличающийся тем, что его осуществляют в барабане с перфорированной поверхностью, в котором частицы Стр.: 1 A R U (57) Формула изобретения 1. Способ уменьшения выделений газа из пористого материала в виде частиц, содержащих неорганическую пористую основу и по меньшей мере 0,1 вес.% одного или нескольких соединений, выбранных из органических соединений, галогенированных соединений, борсодержащих соединений и фосфорсодержащих соединений, согласно которому частицы приводят в движение в пропускаемом через них потоке горячего газа, и на движущиеся частицы распыляют жидкую композицию, содержащую ...

PROCESS FOR LIMITING EMISSIONS OF GASES AND POROUS MATERIAL

a presente invenção a por objeto um processo para limitar as emissões de gases a partir de um material poroso em forma de partículas que compreendem um suporte inorgânico poroso e pelo menos 0,1% em peso de um ou mais compostos escolhido entre os compostos orgânicos, os compostos halogenados, os compostos borados e os compostos fosforados. as partículas são postas em movimento no interior de um fluxo de gás quente que as atravessam, e uma composição líquida que contém um ou mais polímero(s) filmogênio(s) é pulverizada sobre as partículas em movimento por meio de uma bico de atomização bi-fluido no qual a composição líquida é misturada com um gás sob pressão, com uma pressão relativa de atomização superior ou igual a 0,7.105 pa, até a obtenção sobre a superfície das referidas partículas de uma camada protetora que contém o (os) polímero(s) filmogênio(s) e que apresenta uma espessura média inferior ou igual a 20 µm. a presente invenção possui igualmente por objeto um material em forma de partículas recobertas de uma camada protetora, suscetível de ser obtido esse processo. The present invention provides a process for limiting gas emissions from a porous particulate material comprising a porous inorganic support and at least 0.1% by weight of one or more compounds chosen from organic compounds. halogenated compounds, borated compounds and phosphorus compounds. the particles are set into motion within a stream of hot gas flowing therethrough, and a liquid composition containing one or more filmogen polymer (s) is sprayed onto the moving particles by means of a dual atomizing nozzle. a fluid in which the liquid composition is mixed with a pressurized gas having a relative atomization pressure of greater than or equal to 0.7105 pa until a protective layer containing the polymer on the surface of said particles is obtained. (s) filmogen (s) and having an average thickness less than or equal to 20 µm. The present invention also relates to a particulate material coated with ...

Procede de regeneration de catalyseurs de traitement d'hydrocarbures

La présente invention a pour objet un procédé de régénération d'un catalyseur contenant au moins un métal du groupe VIII et au moins un métal du groupe VIB déposés sur un support d'oxyde réfractaire, comportant : - au moins une première étape de traitement thermique du catalyseur, en présence d'oxygène et à une température allant de 350°C à 550°C ; - au moins une seconde étape de dépôt, à la surface du catalyseur, d'un ou plusieurs(s) additif(s) de formule (I) (voir formule I)

Method and apparatus for the regeneration of hydrocarbon synthesis catalysts

The present invention is generally related towards the regeneration of hydrocarbon synthesis catalysts. In particular, the present invention is directed towards the regeneration of deactivated Fischer-Tropsch type catalysts using a two step process wherein the catalyst is first prepared using a dry gas and then regenerated using a hydrogen rich gas. The regeneration process is carried out at temperatures and pressures that are generally different than the operating temperatures and pressures for a typical hydrocarbon synthesis reaction.

Masse active d'oxydo-reduction et procede de combustion en boucle chimique.

L'invention concerne une masse active pour la combustion par oxydo-réduction en boucle chimique qui comprend un liant, sous la forme d'un catalyseur de craquage catalytique en lit fluidisé à base de silice et d'alumine, et une phase active oxyde métallique. La masse active est obtenue par imprégnation de sels métalliques sur le catalyseur de craquage catalytique neuf ou usé.L'invention concerne également un procédé de combustion par oxydo-réduction en boucle utilisant ladite masse active. De manière avantageuse, l'invention s'applique dans le domaine de la captation du C02.

Attrition resistant catalysts and sorbents based on heavy metal poisoned FCC catalysts

A heavy metal poisoned, spent FCC catalyst is treated by chemically impregnating the poisoned catalyst with a new catalytic metal or metal salt to provide an attrition resistant catalyst or sorbent for a different catalytic or absorption processes, such as catalysts for Fischer-Tropsh Synthesis, and sorbents for removal of sulfur gasses from fuel gases and flue-gases. The heavy metal contaminated FCC catalyst is directly used as a support for preparing catalysts having new catalytic properties and sorbents having new sorbent properties, without removing or "passivating" the heavy metals on the spent FCC catalyst as an intermediate step.

Regeneration procedure for Fischer-Tropsch catalyst

A process is disclosed for regenerating catalyst used in a process for synthesizing hydrocarbons. The synthesis process involves contacting a feed stream comprising hydrogen and carbon monoxide with a catalyst in a reaction zone maintained at conversion-promoting conditions effective to produce an effluent stream comprising hydrocarbons. The regeneration. process comprises contacting a deactivated Fischer-Tropsch catalyst with a steam under regeneration-promoting conditions, for a period of time sufficient to reactivate the Fischer-Tropsch catalyst.

System and method for dual fluidized bed gasification

A system, for production of high-quality syngas, comprising a first dual fluidized bed loop having a fluid bed conditioner operable to produce high quality syngas comprising a first percentage of components other than CO and H2 from a gas feed, wherein the conditioner comprises an outlet for a first catalytic heat transfer stream comprising a catalytic heat transfer material and having a first temperature, and an inlet for a second catalytic heat transfer stream comprising catalytic heat transfer material and having a second temperature greater than the first temperature; a fluid bed combustor operable to combust fuel and oxidant, wherein the fluid bed combustor comprises an inlet connected with the outlet for a first catalytic heat transfer stream of the conditioner, and an outlet connected with the inlet for a second catalytic heat transfer stream of the conditioner; and a catalytic heat transfer material.

Catalyst treatment

A cobalt catalyst for use in the Fischer Tropsch reaction of synthesis gas to form hydrocarbons is activated or regenerated by treatment of a cobalt containing catalyst with a gas containing carbon monoxide, said gas containing less than 30% v hydrogen. The catalyst obtained has increased activity and greater selectivity towards producing C5+ hydrocarbons.

催化剂处理

一种关于在将合成气生成烃的费－托法反应中所使用的钴催化剂,该催化剂通过用含一氧化碳的气体对含钴催化剂进行处理而被活化和再生,所说的气体含有少于30%V的氢,该所得到的催化剂提高了活性并且提高了生产C 5 +烃的选择性。

Method of sintering a catalyst