СПОСОБ ПРОВЕДЕНИЯ РЕАКЦИИ ГИДРИРОВАНИЯ НИТРОСОЕДИНЕНИЯ И УСТАНОВКА ПРОВЕДЕНИЯ РЕАКЦИИ ГИДРИРОВАНИЯ

Группа изобретений относится к способу реакции гидрирования нитросоединения и установке проведения реакции гидрирования, которые могут достигать задач непрерывной реакции нитросоединения и длительного цикла регенерации и активации. Способ проведения реакции гидрирования нитросоединения включает в себя этап гидрирования, этап регенерации, этап активации и этап рециркуляции. В зависимости от обстоятельств имеется по меньшей мере один этап, на котором дегазируют регенерированный катализатор, между этапом регенерации и этапом активации. Также заявлена установка проведения реакции гидрирования нитросоединения, применяемая в способе проведения реакции гидрирования нитросоединения, содержащая реактор гидрирования, реактор регенерации, реактор активации и блок рециркуляции. Группа изобретений обеспечивает непрерывную регенерацию и активацию закоксованного катализатора, стабильный цикл производства, реализуемый путем целенаправленного добавления катализатора. 2 н. и 19 з.п. ф-лы, 4 табл., 18 пр.

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Изобретение относится к способу, который позволяет получить регенерированный катализатор дегидрогенизации алкана. Обработка в регенераторе состоит из следующих последовательных стадий: (a) нагревания дезактивированного катализатора до температуры по меньшей мере 660°С с использованием тепла, выделяющегося при сгорании кокса, присутствующего на частично дезактивированном катализаторе, и источника топлива, отличного от указанного кокса; и (b) выдерживание дополнительно дезактивированного катализатора при температуре по меньшей мере 660°С с одновременным воздействием на него потоком кислородсодержащего газа, который по существу не содержит горючих углеводородов, оксидов углерода и паров воды, в течение периода времени, превышающего две минуты. В способе может также (но необязательно) присутствовать стадия (с), на которой осуществляют выдерживание кислородсодержащего регенерированного катализатора со стадии (b) при температуре по меньшей мере 660 °С при одновременном воздействии на регенерированный ...

РЕГЕНЕРАЦИЯ КАТАЛИЗАТОРА

Изобретение относится к области катализа. Описан способ регенерации использованной каталитической смеси, содержащей (i) катализатор изомеризации, содержащий оксид магния, и (ii) катализатор метатезиса, содержащий неорганический носитель и по меньшей мере один компонент из оксида молибдена и оксида вольфрама, включающий: (a) удаление кокса из использованной каталитической смеси в присутствии кислородсодержащего газа, с получением каталитической смеси без кокса; и (b) контактирование каталитической смеси без кокса с паром при температуре в интервале от 100 до 300°C с получением регенерированной каталитической смеси. Технический результат - получение регенерированной каталитической смеси. 5 з.п. ф-лы, 1 табл., 3 пр.

СПОСОБ РЕГЕНЕРАЦИИ ОТРАБОТАННОГО КАТАЛИЗАТОРА ДЛЯГИДРООЧИСТКИ НЕФТЯНОГО СЫРЬЯ

Изобретение относится к регенерации катализаторов для гидроочистки нефтяного сырья на основе оксидов никеля или кобальта, молибдена и алюминия. Регенерацию отработанного катализатора проводят путем термообработки в атмосфере воздуха при температуре 550-600°С в течение 1-1,5 часов, механоактивации с энергонапряженностью не менее 6,6 Вт/г в вибромельнице, размола в порошок, введения при перемешивании смеси, содержащей 3,5-7%-ной концентрации раствора азотной кислоты и солей азотнокислого кобальта или никеля и парамолибдата аммония, формования, сушки и прокаливания. В результате предлагаемый способ регенерации катализатора отличается простотой его проведения, позволяет восстанавливать активность и/или прочность отработанного катализатора. 1 табл.

РЕГЕНЕРАЦИЯ КАТАЛИЗАТОРА ФИШЕРА-ТРОПША ПУТЕМ ЕГО ОКИСЛЕНИЯ И ОБРАБОТКИ СМЕСЬЮ КАРБОНАТА АММОНИЯ, ГИДРОКСИДА АММОНИЯ И ВОДЫ

Изобретение относится к области катализа. Описан способ регенерирования одной или более частиц кобальтсодержащего катализатора Фишера-Тропша in situ в реакторной трубе, включающий стадии: (i) окисление частицы (частиц) катализатора при температуре от 20 до 400°C; (ii) обработку частицы (частиц) катализатора в течение более 5 мин растворителем; (iii) сушку частицы (частиц) катализатора; и (iv) необязательно восстановление катализатора водородом или каким-либо водородсодержащим газом. Технический результат - повышение активности катализатора. 9 з.п. ф-лы, 4 табл., 4 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 ...

СПОСОБ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРА ДЛЯ ПОЛУЧЕНИЯ ИЗОПРЕНА ИЗ 4,4-ДИМЕТИЛ-1,3-ДИОКСАНА

Изобретение относится к способам регенерации катализаторов, в частности кальцийфосфатных, и может быть использовано в нефтехимической промышленности для производства изопрена. Описан способ, согласно которому регенерация катализатора для получения изопрена из 4,4-диметил-1,3-диоксана проводится путем выжига кокса и смол при температуре 400-550°С паровоздушной смесью периодически в спаренных, параллельно работающих на контактировании реакторах, которые при регенерации включают последовательно, и регенерация катализатора в первом по ходу реакторе проходит при давлении 2,2-2,8 ати, затем газы регенерации охлаждают до 380-450°С в узле регулирования температуры газов регенерации и направляют полностью или частично во второй по ходу реактор, работающий под давлением 0,9-1,1 ати и далее в атмосферу. Технический результат: способ позволяет проводить регенерацию катализаторов со снижением удельного расхода водяного пара. 1 табл., 1 ил.

СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ ЛЕГКИХ ОЛЕФИНОВ

Использование: для получения пропилена, бутиленов и пентенов, а также высокооктановой фракции бензина с низким содержанием бензола путем каталитической конверсии легкого, тяжелого газойля, геройля вакуумной перегонки или нафты при использовании обычных или усовершенствованных катализаторов ФКК. Сущность изобретения: способ включает стадии подачи углеводородного исходного материала в реакционную зону, содержащую твердый катализатор, контактирование углеводородного исходного материала в реакционной зоне с катализатором, в условиях, которые благоприятствуют каталитической конверсии углеводородов в легкие олефины, отделение полученных продуктов реакции из реакционной зоны после каталитической конверсии, выделение катализатора и регенерацию дезактивированного катализатора в регенераторе. В соответствии с изобретением углеводородный исходный материал контактирует с катализатором в реакторе с циркулирующим флюидизированным слоем при времени пребывания в диапазоне от 0,1 до 3 с. Изобретение позволяет ...

СПОСОБ ПЕРЕРАБОТКИ ГАЗОВОГО КОНДЕНСАТА

Изобретение относится к нефтехимической промышленности и касается получения высококачественных моторных топлив из газового конденсата. Описан способ переработки газового конденсата, включающий его предварительный нагрев в соответствующих технологических аппаратах, контактирование в адиабатическом реакторе при температуре 320-480°С и давлении 0,1-4 МПа с цеолитсодержащим катализатором, охлаждение и разделение продуктов реакции на газообразные и жидкие фракции путем сепарации и ректификации с последующей окислительной регенерацией катализатора, причем перед процессом регенерации проводят удаление тяжелых смол, накопленных на катализаторе, путем вакуумирования адиабатического реактора в течение 0,5-6,0 ч, а регенерацию катализатора осуществляют в регенераторе при температуре 350-620°С и давлении 0,1-0,2 МПа воздухом с содержанием кислорода 21 об.%, который подают после прогрева верхнего или нижнего слоя катализатора, причем со стороны, противоположной нагретому слою. Технический результат ...

ОЧИЩАЮЩИЙ ОТ ДИСПЕРСНЫХ ЧАСТИЦ МАТЕРИАЛ, ФИЛЬТР-КАТАЛИЗАТОР ДЛЯ ОЧИСТКИ ОТ ДИСПЕРСНЫХ ЧАСТИЦ С ИСПОЛЬЗОВАНИЕМ ОЧИЩАЮЩЕГО ОТ ДИСПЕРСНЫХ ЧАСТИЦ МАТЕРИАЛА И СПОСОБ РЕГЕНЕРИРОВАНИЯ ФИЛЬТРА-КАТАЛИЗАТОРА ДЛЯ ОЧИСТКИ ОТ ДИСПЕРСНЫХ ЧАСТИЦ

Изобретение относится к очищающему от дисперсных частиц материалу и его использованию. Описан очищающий от дисперсных частиц материал, используемый для фильтра-катализатора для очистки от дисперсных частиц, причем фильтр-катализатор расположен на пути потока выхлопных газов двигателя внутреннего сгорания, улавливает дисперсные частицы в выхлопных газах, образующихся в двигателе внутреннего сгорания, и сжигает осаждаемые дисперсные частицы с тем, чтобы регенерироваться, причем очищающий от дисперсных частиц материал включает в себя: оксид, содержащий: церий (Се), обладающий способностью аккумулирования-высвобождения кислорода; и по меньшей мере один металл (Me), выбранный из группы, состоящей из циркония (Zr), иттрия (Y), лантана (La), празеодима (Рr), стронция (Sr), ниобия (Nb) и неодима (Nd), при этом отношение содержаний (Се:Ме) церия к металлу составляет от 6:4 до 9:1 в единицах атомного отношения, и степень кристалличности (CR), представленная следующей формулой (1), составляет в пределах ...

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 реактивации катализатора гидроочистки

Предложен способ реактивации катализатора гидроочистки, по которому отработанный катализатор после окислительной регенерации пропитывают раствором лимонной и ортофосфорной кислот в смеси воды и бутилдигликоля, имеющим концентрации бутилдигликоля 10-20 об.%, лимонной кислоты 0,42-1,09 моль/л, ортофосфорной кислоты 0,17-0,54 моль/л, далее подвергают термообработке при температуре 60-90С в течение 20-60 мин, затем сушат на воздухе при температуре 100-220С в течение 2-6 ч, в результате получают катализатор, имеющий объем пор 0,3-0,55 мл/г, удельную поверхность 120-180 м/г, средний диаметр пор 7-12 нм и содержащий, мас.%: Ni(CHO) – 8,8-15,6; H[Mo(СНO)O] – 3,2-8,0; H[PNiMoO] – 5,8-11,6; H[Ni(OH)MoO] – 3,7-7,1; H[PMoO] – 3,0-7,4; носитель – остальное; при этом носитель содержит мас.%: SO– 0,5-2,5; PO– 2,5-5,5; γ-AlO– остальное; что соответствует содержанию в сульфидированных катализаторах, мас.%: Мо – 10,0-16,0; Ni – 2,5-4,5; P – 1,2-2,4; S – 6,7-10,8; γ-AlO– остальное. Технический результат - ...

СПОСОБ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРА ЦИКЛИЗИРУЮЩЕГО ГИДРОЛИЗА АМИНОНИТРИЛА В ЛАКТАМ И ИСПОЛЬЗОВАНИЕ РЕГЕНЕРИРОВАННОГО КАТАЛИЗАТОРА ДЛЯ ПРОИЗВОДСТВА ЛАКТАМОВ

... 1. Способ регенерации катализатора циклизирующего гидролиза аминонитрила в лактам, в котором катализатором является твердый оксид, отличающийся тем, что катализатор обрабатывают при температуре от 300 до 600°С в окислительной атмосфере. 2. Способ по п.1, отличающийся тем, что окислительная атмосфера содержит по меньшей мере 2 об.% кислорода. 3. Способ по п.1 или 2, отличающийся тем, что окислительная атмосфера представляет собой смесь кислорода с инертным газом или воздуха с инертным газом. 4. Способ по п.2 или 3, отличающийся тем, что инертный газ выбирают из группы, в которую входят азот, благородные газы, углекислый газ и водяной пар. 5. Способ по одному из пп.1-4, отличающийся тем, что концентрацию кислорода в окислительной атмосфере постепенно увеличивают в процессе обработки катализатора. 6. Способ по одному из пп.2-5, отличающийся тем, что концентрация кислорода в окислительной атмосфере составляет от 1 до 10% по объему. 7. Способ по одному из пп.1-6, отличающийся тем, что температура ...

СПОСОБ ПОЛУЧЕНИЯ ФТОРЗАМЕЩЕННОГО (ГАЛОГЕНСОДЕРЖАЩЕГО) УГЛЕВОДОРОДА

Способ получения фторзамещенного (галогенсодержащего) углеводорода включает контактирование α-фторзамещенного простого эфира в паровой фазе при повышенной температуре с катализатором и катализатор обрабатывают для поддержания и/или восстановления его активности. Обработка катализатора включает либо нагревание катализатора до повышенной температуры, превышающей примерно 250C, при отсутствии a-фторзамещенного простого эфира, либо контактирование катализатора при повышенной температуре с окисляющим веществом в период или между периодами контактирования a-фторзамещенного простого эфира с катализатором. Катализатор может представлять собой промотирующий окисление металл, например цинк, железо или медь, нанесенный на подложку из оксида, фторида или оксифторида металла.

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.

СПОСОБ ОБРАБОТКИ СИСТЕМЫ КАТАЛИТИЧЕСКИХ РЕАКТОРОВПЕРЕД ПРОВЕДЕНИЕМ ТЕХНИЧЕСКОГО ОБСЛУЖИВАНИЯ РЕАКТОРОВ

... 1. Способ проведения технического обслуживания для системы каталитических реакторов, включающий уменьшение уровня содержания в системе каталитических реакторов, по меньшей мере, одного вредного вещества, включающего бензол, где активность содержащегося в системе катализатора после проведения технического обслуживания согласно измерению Т-экв. находится в пределах отклонения приблизительно на 11°С (20°F) от активности катализатора до проведения технического обслуживания. 2. Способ по п.1, где уменьшение уровня содержания, по меньшей мере, одного вредного вещества включает окисление, по меньшей мере, одного вредного вещества. 3. Способ по п.2, где окисление, по меньшей мере, одного вредного вещества происходит при температуре в диапазоне от приблизительно 177°С (350°F) до приблизительно 260°С (500°F). 4. Способ по п.1, где уменьшение уровня содержания, по меньшей мере, одного вредного вещества происходит до безопасного уровня воздействия. 5. Способ по п.2, дополнительно включающий отслеживание ...

Способ получения масляного альдегида

Изобретение касается производства альдегидов, в частности масляного альдегида , который используют для синтеза бутиловых спиртов, Цель - увеличение активности катализатора. Процесс ведут реакцией гидИзобретение относится к способу получения масляного альдегида и касается способа обработки реакционной среды реакции гидроформилирования пропилена при получении масляного альдегида т.е к способу селективного превращения алкилзамещен- ных фосфинов, содержащихся в реакционной среде реакции гидроформирования пропилена , в соответствующие окислы фосфинов роформилирования пропилена моноокисью углерода и водородом в присутствии катализатора , представляющего собой смесь родия с трифенилфосфином, с образованием реакционной массы, содержащей масляный альдегид, высококипящие побочные продукты конденсации масляного альдегида, пропилдифенилфосфин, трифенилфосфин и остальную часть, содержащую комплексный родиевый катализатор, трифенилфосфинок- сид и высококипящие органические компоненты , с последующей ...

Способ регенерации платинусодержащего катализатора риформинга

Изобретение касается каталитической химии, в частности регенерации платинусодержащего катализатора ри- форминга, что может быть использовано в нефтехимии. Цель - повышение экономичности способа. Его ведут пропусканием закоксованного катализатора сверху вниз в зону регенерации в виде плотного слоя, контактированием катализатора с кислородсодержащим газом в зоне горения, расположенной внутри зоны регенерации, до полного выжига углерода. Образовавшиеся газообразные продукты сгорания удаляют из зоны регенерации. При этом часть газового потока подвергают сжатию с получением газового потока с повышенным давлением, из которого потока направляют в зону нагрева, расположенную после зоны горения, где он контактирует с обезуглерешенным катализатором, поступившим из зоны горения. Остальную часть газового потока охлаждают и направляют в зону горения в качестве кислородсодержащего газа. Обезуглероженный катализатор пропускают через зону хлорирования , расположенную в зоне регенерации , и контактируют ...

KATALYTISCHE DAMPFPHASEN-OXYDATION VON n-BUTAN ZU MALEINSÄUREANHYDRID EINSCHLIESSEND IN-SITU CALCINATION/AKTIVIERUNG DES KATALYSATORS

REGENERIERUNG VON KATALYSATOREN FÜR DIE HYDRIERUNG VON KOHLENSTOFFMONOXID

Regenerierung von verbrauchtem FCC-Katalysator

Kontinuierliches Verfahren zur katalytischen Umwandlung von organischen Einsatzmaterialien

AKTIVIERUNG UND REGENERIERUNG EINES HYDRO-OXYDIERUNGSKATALYSATORS

VERFAHREN ZUR FÜHRUNG DER UMSETZUNG EINES STROMES VON C4+ UND SCHWEREREN KOHLENWASSERSTOFFEN ZU NIEDRIGEREN PRODUKTEN BEI DER UMSETZUNG VON SAUERSTOFFVERBINDUNGEN

KATALYTISCHES VERFAHREN ZUR HERSTELLUNG VON LEICHTEN OLEFINEN AUS METHANOL IN EINEM FLUIDISIERTEN BETTREAKTOR

Catalysts

REGENERATION PROCESS FOR A FISCHER-TROPSCH CATALYST

Process for the regeneration of a catalyst used for the preparation of hydrocarbons by catalytic reaction of carbon monoxide with hydrogen, comprising the steps of: (i) washing the catalyst with hydrocarbons; (ii) drying the washed catalyst; (iii) treating the dried catalyst at elevated temperature with a gas containing about 0.1-3 % by vol oxygen. The washing may occur in two stages, the first at 100-170 DEG C being with paraffin, the second at 20-90 DEG C being with naphtha or hexane. The oxygen in stage (iii) may be diluted with nitrogen. Specified catalyst components are cobalt with ruthenium on a carrier of silica and/or alumina. Zr, Ti or Cr may be included, singly or in combination.

Improvements relating to the regeneration of fouled catalysts

... 554,691. Regenerating catalysts. GAS LIGHT & COKE CO., GRIFFITH, R. H., PLANT, J. H. G., and INMAN, C. J. Dec. 15, 1941, No. 16176. [Class 1 (i)] Catalysts are regenerated in a stationary bed in a well-lagged vessel heated at one end to initiate combustion and into which a current of air is passed at that end at just sufficient velocity to cause a restricted hot zone to travel through the bed in the same direction as the stream of gas. The apparatus comprises a lagged cylinder a with removable cover d provided with an air supply pipe e and electrical heating element f. The combustion products are withdrawn through perforations m, and the catalyst when regenerated is removed through valve c.

Improvements in or relating to a method of controlling the water content of a regenerated finely-divided catalyst

In the regeneration of a catalyst in the form of a dense fluidized bed 12 with an oxidizing gas to burn off carbonaceous deposits, the water content of the regenerated catalyst is controlled by passing a major proportion of the catalyst from the fluidized bed through a first stripping zone 24 in countercurrent with a dry inert gas introduced at 26, passing a minor proportioh via openings 32 through a second stripping zone 30, within and in heat exchange relationship with the fluidized bed, and contacting the minor proportion of catalyst at elevated temperature in countercurrent flow with dry inert gas introduced at 34, stripping in zone 30 being for a substantially longer time than in zone 24 in order to remove substantially all the moisture from the catalyst; streams of catalyst from the two stripping zones are combined in line 28 to produce a regenerated catalyst having a desired water content. Regeneration of a hydroforming catalyst is described, catalyst being introduced ...

Recovery of energy in flue gases from a regeneration zone by means including a turbine-compressor combination

... 1,003,517. Steam and gas turbine plant; generating combustion products under pressure. PULLMAN Inc. Nov. 27, 1961, No. 42286/61. Headings F1G and F1L. [Also in Division B1] In the supply of regeneration gases to a regeneration zone, a method of utilizing flue gases recovered from the regeneration zone comprises recovering the flue gases at an elevated temperature, removing finely divided particle material from the gases, expanding the gases in a turbine to provide power to drive a compressor which compresses regeneration gas to a suitable elevated pressure for passage to the regeneration zone, and recovering the expanded flue gases from the turbine at an elevated temperature for the generation of steam employed in a steam turbine to provide a portion of the power required to drive the compressor. Coke is burnt in a regenerator 22 to burn off carbonaceous deposits on a fluidized catalyst material 20. The resulting flue gases are passed through cyclone separators 28, 30 wherein some of the ...

Improvements in carrying out gas reactions

In a process in which gas reactions are carried out with the aid of a fluidized catalyst, the catalyst is continuously circulated between the reactor (under reduced pressure) and a regenerator (at a higher pressure) wherein it is regenerated by oxygen-containing gas and heated; the system comprises auxiliary circulation by which the catalyst is conveyed from the regenerator to an intermediate container before passing to the reactor. The means of conveyance is a gas, preferably the gas used in the reaction. The following features are preferred: (a) the catalyst particle size is 1-300, particularly 20-100 microns; (b) the reactor pressure 0.05-0.5, particularly 0.1-0.3 atmos., and the regenerator pressure about 1-3 atmos. The catalyst may be for example Al2O3 (activated by e.g. Cr2O3, MoO3, WO3, ZnO, BeO, Cu, Ni, Co, Pd or Pt) activated iron catalysts, phosphates, natural or synthetic activated silicates; in the example it is Al2O3 with 18% Cr2O3, particle size 50-100 m . The following are ...

Improved method and apparatus for catalyst activation

... In a process for activating solid catalyst particles wherein the catalyst is contacted with a stream of inert gas at an activation temperature and at a velocity sufficient to maintain the catalyst in a fluidized state, the stream of gas is maintained in a closed recirculating system, make-up gas is added to the recirculating stream at a predetermined rate and gas is purged from the stream at a rate equal to the make-up gas rate so that a circulation rate may be maintained independently of the make-up and purge rates. Catalyst to be activated, such as chromium oxide impregnated on a silica-alumina base is conveyed to a fluidizing zone 12 of a vessel 11 where it rests on a grid 15 and is fluidized by air from blowers 22 and 22a passing through a line 23, inlet 17 and outlet 18. Entrained catalyst is removed from the airstream in a disengaging zone 13 of larger area to reduce the velocity of the air. The air from outlet 18 passes through a cyclone separator 19 and is returned ...

FCC electrolyser system

A system comprising a regenerator 2 for regenerating a catalyst from a fluid catalytic cracking unit and at least one solid oxide electrolyser cell 36, wherein the regenerator 2 has an infeed for receiving an oxygen supply for enabling regeneration of the catalyst for reuse in the cracking unit by burning of catalyst coke off the catalyst, and the at least one oxide electrolyser cell 36 comprises an anode, a cathode and an electrolyte, a steam input 42, and an oxygen rich gas output 56 which connects to the infeed of the regenerator 2. A heat exchanger 58 may be in fluid flow communication with both the oxygen rich gas output 56 and a gas infeed for the solid oxide electrolyser 36 for exchanging heat between an oxygen rich gas stream 46 from the oxygen rich gas output and a feed gas for the gas infeed such as an air, nitrogen stream or steam feed. A method for regenerating a catalyst from a fluid catalytic cracking unit and a fluid catalytic cracking system comprising a fluid catalytic ...

PROCESS FOR REGENARATING A COBALT COMPRISING FISCHER-TROPSCH CATALYST

Process for regenarating a cobalt comprising fischer-tropsch catalyst

Process for regenarating a cobalt comprising fischer-tropsch catalyst

Process for regenarating a cobalt comprising fischer-tropsch catalyst

PROCEDURE FOR THE IMPROVEMENT OF A CATALYST

A ON AN INFLAMMABLE BONDING AGENT OF BASING MIXTURE METAL CATALYST

PROCEDURE FOR THE DISTANCE OF CARBON DEPOSITS IN A HEAT EXCHANGER

GAS CELL SYSTEM AND ASSOCIATED OPERATING PROCEDURE

PROCEDURE FOR the PRODUCTION OF 3,4-EPOXY-1-BUTEN

PROCESS CONDITIONS FOR THE ENTERPRISE OF AN IGNITION CATALYST FOR THE BURN OF NATURAL GAS.

PROCEDURE FOR REGENERATING COKE-POLLUTED CATALYST.

VERY LOW-TEMPERATURE RECOVERY OF REFORMATION CATALYSTS DEACTIVATED BY COKE

PROCEDURE FOR THE REGENERATION OF CATALYSTS.

HYDROFORMYLIERUNGSVERFAHREN

FISCHER TROPSCH PROCEDURE WITH IMPROVED CATALYST RECOVERY

PROCEDURE AND DEVICE FOR THE CONTINUOUS TRANSFORMATION OF HYDROCARBONS

CARRIER CATALYST TREATMENT

EPOXYSYNTHESE WITH RECOVERY THAT TITANSILIKALITKATALYSATOREN

PROCEDURE FOR THE RECOVERY OF A ZEOLITE OF CATALYST

REGENIERUNGSVERFAHREN A CATALYST FOR CYCLISIERENDEN THE HYDROLYSIS OF A AMINONITRILS IN LACTAM AND USE OF THE REGENIERTEN CATALYST FOR LACTAM PRODUCTION

PROCEDURE FOR THE EX INTERNATIONAL TELECOMMUNICATION UNION REGENERATION OF PRECIOUS METAL CONTAINING CATALYSTS

Process for activating a reforming catalyst

PASSIVATION OF VANADIUM CONTAMINANTS OF CATALYTIC CRACKING CATALYSTS

Process for the conversion of an olefin or a mixture of olefins

Process for the regeneration of reforming catalysts

Process for regenerating and rejuvenating additive containing catalysts

Process for the reactivation of sulfur deactivated cobalt titania catalyst

PROCESS FOR THE REMOVAL OF H2S FROM A SOUR GASEOUS STREAM

K 7582 II PROCESS FOR THE REMOVAL OF H2S FROM A SOUR GASEOUS STREAM Process for the removal of H2S from a sour gaseous stream comprising contacting the sour gaseous stream with aqueous reactant solution in contacting zone (2) at a temperature below the melting point of sulphur, the reactant solution containing solubilized coordination complex of Fe (III) with nitrilotriacetic acid under conditions to convert H2S, producing a gaseous stream having reduced H2S content, and aqueous mixture containing solid sulphur and an increased concentration of solubilized coordination complex of Fe (II) with nitrilotriacetic acid, removing aqueous mixture from the contacting zone (2) and separating a minor portion of the mixture having an increased solid sulphur concentration, heating mixture having an increased sulphur concentration in an at least substantially oxygen free environment (10) to a temperature sufficient to melt the sulphur to produce a solution of solubilized coordination complexes of iron ...

PROCESS FOR THE FLUID CATALYTIC CRACKING OF A HYDROCARBON FEEDSTOCK

PROCESS FOR THE FLUID CATALYTIC CRACKING OF A HYDROCARBON FEEDSTOCK A process for the fluid catalytic cracking of a hydrocarbon feedstock in a reactor system comprising an endothermic cracking zone (6, 7) and an exothermic regeneration zone (13), wherein heat is exchanged between said zones not only by the circulation of catalyst (5, 6, 11), but also by passing the fresh feedstock (1) through heat exchange coils (16) in the regeneration zone (13.) before contacting hot regenerated catalyst in a liftpot (4) and entering the reaction zone (6, 7). The temperature in the regeneration zone is thus kept below 725.degree.C, whereas the feedstock is preheated to at least 200.degree.C, preferably to 325-400.degree.C. Heavy and high metal-containing feedstocks may be processed in this way. Fig. 1 ...

REACTIVATION OF VANADIUM-CONTAINING OXIDATION CATALYSTS

O.Z. 0050/34985 A process for reactivating a vanadium-containing oxidation catalyst, wherein the catalyst is treated first at from 100 to 600.degree.C, with a volatile phosphorus compound in the presence of an oxygen-containing gas, and then at from 50 to 600.degree.C with sulfur trioxide or a mixture of a volatile sulfur compound and an oxygen-containing gas.

PROCESS FOR REDUCING CO AND SO.SUB.X EMISSIONS FROM CATALYTIC CRACKING UNITS

... " " Reduction of CO and SOx emissions from regenerators associated with cyclical fluidized catalytic cracking (FCC) units used to convert hydrocarbon feedstocks into more valuable products is achieved by introducing particles of bastnaesite into the FCC unit. The bastnaesite particles recycle with the catalyst particles successively through a catalytic cracking reaction zone, a stripping zone, and a regeneration zone. The bastnaesite particles react with SOx produced in the regeneration zone of the FCC unit, thereby lowering the SOx content of the flue gas discharged therefrom. in the catalytic cracking and stripping zones of the FCC unit, the bastnaesite particles are at least partially reactivated so that upon returning to the regeneration zone yet more SO2 is removed. The bastnaesite particles also aid in lowering CO emissions from the FCC regenerator by catalysing the reaction between CO and oxygen to yield Co2.

FLUID CATALYTIC CRACKING CRYSTALLINE ALUMINOSILICATE CATALYSTS

HYDROCARBON CONVERSION CATALYST CONTAINING A CO OXIDATION PROMOTER

A cracking catalyst for promoting the oxidation of carbon monoxide to carbon dioxide during regeneration of the catalyst by the burning of coke therefrom, which comprises a crystalline aluminosilicate zeolite, an inorganic porous oxide matrix material and CO oxidation promoter, such as a Group VIII metal or compound thereof. The catalyst is preferably prepared by first supporting the CO oxidation promoter on an inorganic porous oxide base, such as alumina or ultra-stable variety of Y-type zeolite, and thereafter embedding the supported CO oxidation promoter and a crystalline aluminosilicate zeolite, such as rare earth metal exchanged X- or Y-type zeolite, in an inorganic porous oxide matrix material, such as silicaalumina or clay.

ON-LINE REGENERATION OF HYDRODESULFURIZATION CATALYST

ALUMINA BOUND CATALYST FOR SELECTIVE CONVERSION OF OXYGENATES TO AROMATICS

A catalyst composition comprising a zeolite, an alumina binder, and a Group 12 transition metal selected from Zn and/or Cd, the zeolite having a Si/Al ratio of at least about 10 and a micropore surface area of at least about 340 m2/g, the catalyst composition comprising about 50 wt% or less of the binder, based on a total weight of the catalyst composition, and having a micropore surface area of at least about 290 m2/g, a molar ratio of Group 12 transition metal to aluminum of about 0.1 to about 1.3, and at least one of: a mesoporosity of about 20 m2/g to about 120 m2/g; a diffusivity for 2,2-dimethylbutane of greater than about 1 x 10-2 sec-1 when measured at a temperature of about 120°C; and a 2,2-dimethylbutane pressure of about 60 torr (8kPa); and a combined micropore surface area and mesoporosity of at least about 380m2/g.

CATALYST FOR SELECTIVE CONVERSION OF OXYGENATES TO AROMATICS

A catalyst composition comprises a self-bound zeolite and a Group 12 transition metal selected from the group consisting of Zn, Cd, or a combination thereof, the zeolite having a silicon to aluminum ratio of at least about 10, the catalyst composition having a micropore surface area of at least about 340 m2/g, a molar ratio of Group 12 transition metal to aluminum of about 0.1 to about 1.3, and at least one of: (a) a mesoporosity of greater than about 20 m2/g; and (b) a diffusivity for 2,2-dimethylbutane of greater than about 1 x 10-2 sec-1 when measured at a temperature of about 120°C and a 2,2-dimethylbutane pressure of about 60 torr (about 8 kPa).

REGENERATION OF SPENT PARAFFIN DEHYDROGENATION CATALYST

There is provided a method for regenerating a spent dehydrogenation catalyst used in the conversion of n-paraffin to olefin. The method comprises method steps for removing the coke by treating the catalyst with an ozone-oxygen stream followed by an oxygen stream. The catalyst is stabilized by passing a nitrogen stream and the stabilized catalyst is rejuvenated by passing an air-nitrogen stream containing a halogenated hydrocarbon. This is followed by reducing the metal oxide in the catalyst by passing hydrogen-nitrogen stream.

PROCESS AND APPARATUS FOR DISTRIBUTING FLUIDS IN A CONTAINER

Process for radial distribution of fluid into a fluid mass wherein fluid is radially conveyed within and isolated from the fluid mass and discharged via a plurality of distribution points located radially in the fluid mass.

SULFUR DIOXIDE REGENERATION OF SUPERACID CATALYST

A process for regeneration of spent sulfated and calcined solid superacid catalyst is disclosed. Said process comprises heating said catalyst to a temperature of approximately 450.degree.C and contacting said catalyst with a gas stream comprising oxygen or air and sulfur dioxide. This regeneration process can be performed in situ.

FCCU REGENERATOR CATALYST DISTRIBUTION SYSTEM

Disclosed are devices for introducing and uniformly distributing spent catalyst into a regenerator bed of a fluid catalytic cracking unit. Also disclosed are devices for collecting and discharging regenerated catalyst from the regenerator bed. The devices provide more uniform contacting of the spent catalyst particles with regeneration gas and and consequently more efficient and complete regeneration.

PROCESS FOR REGENERATING OFF SITE A CATALYST CONTAINING AT LEAST ONE PRECIOUS METAL

Procédé de régénération d'un catalyseur usé de traitement d'hydrocarbures comprenant au moins un métal précieux choisi dans le groupe formé par l'argent, l'or, le ruthénium, le rhodium, le palladium, l'osmium, l'iridium et le platine, et au moins un support poreux. Le procédé comprend au moins les deux étapes successives suivantes: au moins une étape de combustion du coke présent sur ledit catalyseur en présence d'un gaz comprenant de l'oxygène, à température comprise entre 300 et 680.degree.C et pour une durée comprise entre 0,3 et 7 heures, et au moins une étape d'oxyhalogênation sous atmosphère contrôlée d'air, à une température comprise entre 300 et 650.degree.C, pour une durée comprise entre 0, 3 et 3 heures et en présence d'un composé halogéné. Le procédé est effectué hors site, en ce que l'on utilise pour l'étape de combustion et pour l'étape d'oxyhalogénation un four à lit mobile.

Verfahren zum Verbinden von Blechpartien.

Verfahren zur Herstellung von normalerweise gasförmigen Olefinen

Verfahren und Vorrichtung zum Oxydieren von reduzierten Katalysatoren

Verfahren und Vorrichtung zur Durchführung chemischer Reaktionen mit einer Schmelze als wärmeübertragendes Medium

Verfahren zur Regenerierung eines Katalysators

Verfahren zur Regenerierung eines Katalysators in einem Rohrkonverter

PROCEDURE FOR THE CATALYTIC CRACKEN OF A HYDROCARBON FILLING IN A FLUIDISED BED.

CONVERSION OF OXYGEN-CONTAINING SUBSTANCES IN OLEFINS OVER CATALYST, INCLUDING ACID MOLECULAR SIEVE WITH REGULIROVANNYMSOOTNOShENIM BETWEEN CARBON ATOM OF AND ACID SECTION

METHOD OF REGENERATION OF HYDROGENATION CATALYST

СПОСОБ ОБНОВЛЕНИЯ КАТАЛИЗАТОРА ГИДРООЧИСТКИ

Описан способ обновления катализатора гидроочистки, содержащего гидрирующий металл группы VIB и/или гидрирующий металл группы VIII, который включает стадии: (a) регенерации катализатора путем введения во взаимодействие указанного катализатора с содержащим кислород газом при температуре, примерно равной от 300 до 550°C, (b) пропитки регенерированного катализатора с уменьшенным содержанием углерода пропитывающим раствором, который содержит смесь воды и комбинации MoO3 и H3PO4, (с) выдерживания пропитанного катализатора и (d) сушки выдержанного катализатора. Также описан полученный обновленный катализатор и его применение для гидроочистки углеводородного сырья.

СПОСОБ ОБНОВЛЕНИЯ КАТАЛИЗАТОРА ГИДРООЧИСТКИ

Описан способ обновления катализатора гидроочистки, содержащего гидрирующий металл группы VIB и/или гидрирующий металл группы VIII, который включает стадии: (a) регенерация катализатора путем введения во взаимодействие указанного катализатора с содержащим кислород газом при температуре, примерно равной от 300 до 550°C, с получением регенерированного катализатора с уменьшенным содержанием углерода, (b) пропитка регенерированного катализатора с уменьшенным содержанием углерода раствором, который содержит смесь воды и лимонной кислоты, (c) выдерживание пропитанного катализатора в течение не менее 6 ч и (d) сушка выдержанного катализатора. В изобретении также описан полученный обновленный катализатор и его применение для гидроочистки углеводородного сырья.

METHOD OF OXIDATIVE DEHYDROGENATION OF N - BUTENES IN BUTADIENE

METHOD OF OXIDATIVE DEHYDROGENATION OF N-BUTENES IN 1.3-BUTADIENE

METHOD OF STABILIZATION OF CATALYST ACTIVITY DURING THE WORK OF INSTALLATION MVO

SYNTHESIS FISCHER - TROPSCH

ИНТЕГРАЦИЯ В РЕАКЦИОННУЮ СИСТЕМУ ДЛЯ КИСЛОРОДСОДЕРЖАЩЕГО ВЕЩЕСТВА-В-ОЛЕФИНЫ УСТАНОВКИ РАЗДЕЛЕНИЯ ВОЗДУХА

В заявке описаны объединенная система и способ получения легких олефинов и полимеров из кислородсодержащих веществ и необязательно из природного газа. Эта объединенная система включает установку разделения воздуха, которая разделяет компоненты воздуха на поток кислорода и поток азота и которая образует также поток сжатого воздуха. В соответствии с настоящим изобретением поток кислорода, поток азота и/или поток сжатого воздуха из установки разделения воздуха могут служить в качестве реагента в процессе генерирования синтез-газа, в качестве регенерационной среды в реакционной системе для метанола-в-олефины, в качестве псевдоожижающего потока, в качестве создающей защитную атмосферу среды, в качестве отделяющей среды, в качестве пневматического средства и/или в качестве реагента в установке удаления серы.

СПОСІБ РЕГЕНЕРАЦІЇ КАТАЛІЗАТОРА ДЛЯ ЦИКЛІЗУЮЧОГО ГІДРОЛІЗУ АМІНОНІТРИЛУ В ЛАКТАМИ ТА СПОСІБ ОДЕРЖАННЯ ЛАКТАМІВ ЦИКЛІЗУЮЧИМ ГІДРОЛІЗОМ

Заявлений винахід відноситься до способу регенерації каталізатора для циклізуючого гідролізу амінонітрилу для одержання лактамів. Більш детально, він відноситься до регенерації твердих каталізаторів, які використовуються в процесах одержання лактамів циклізуючим гідролізом амінонітрилів. Цей регенераційний процес полягає в обробці використаного каталізатора в кінці циклу при температурі в межах від 300 до 600°С в окиснювальному середовищі.

СПОСОБ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРОВ ДЕГИДРИРОВАНИЯ АЛКАНОВ

Изобретение относится к способу дегидрирования алканов, по которому алкан в реакторе дегидрирования алканов подают через катализатор, причем процесс можно проводить адиабатически или неадиабатически, катализатор дегидрирования после фазы реакции регенерируют посредством перепуска газа, причем этот газ после короткой фазы продувки водяным паром подают через катализатор, и этот регенерационный газ состоит из кислородсодержащего газа и пара, и катализатор после регенерации освобождают от кислородсодержащего газа посредством перепуска газа, причем продолжительность времени перепуска кислородсодержащего газа по сравнению с обычным способом заметно сокращается и составляет 70% или меньше от полной длительности регенерации, катализатор после проведения регенерации при постоянной активности имеет повышенную селективность к образованию алкена, и катализатор состоит из металла группы платиновых металлов или металлов группы VIB периодической системы элементов, который в форме соединения или в элементной ...

СПОСОБ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРА РИФОРМИНГА

Настоящее изобретение относится к способу регенерации катализатора для получения ароматических углеводородов или для риформинга. Указанный способ содержит стадию горения в зоне А, содержащей, по меньшей мере, 2 слоя А1 и А2, стадию оксихлорирования в зоне В и стадию прокаливания в зоне С. Часть газа, выходящего из зоны оксихлорирования, рециркулируется через, по меньшей мере, одну секцию газоочистки D к впуску в слои А1 и А2. Кроме того, часть газа, выходящего из зоны В, рециркулируется в слой горения А2, проходя через газодувку, но без прохождения через указанную секцию газоочистки D.

СПОСОБ И ЕМКОСТЬ ДЛЯ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРА РИФОРМИНГА

Настоящее изобретение относится к способу регенерации катализатора для получения ароматических углеводородов или для риформинга, причем способ содержит стадию горения в зоне А, содержащей, по меньшей мере, 2 слоя А1 и А2, стадию оксихлорирования в зоне В и стадию прокаливания в зоне С. Часть газа, выходящего из зоны оксихлорирования, рециркулируется через, по меньшей мере, одну секцию газоочистки D к впуску в слои А1 и А2. Кроме того, часть газа, выходящего из зоны В, рециркулируется в слой горения А2, проходя через газодувку, но без прохождения через указанную секцию газоочистки D, и часть рециркулируется к впуску в зону В, проходя через указанную газодувку, но не через указанную секцию газоочистки. Настоящее изобретение также относится к емкости, в которой осуществляется указанный способ.

СИНТЕЗ ФИШЕРА-ТРОПША

Способ (10) синтеза продуктов (20) Фишера-Тропша предусматривает подачу синтез-газа (30) в реактор (16) синтеза Фишера-Тропша с подвижным слоем, содержащий катализатор синтеза Фишера-Тропша в подвижном слое катализатора, и каталитическое превращение по меньшей мере части синтез-газа (30) в подвижном слое катализатора в продукты (20) Фишера-Тропша. Продукты (20) Фишера-Тропша отводят из реактора (16) синтеза Фишера-Тропша с подвижным слоем. Способ (10) также предусматривает, когда реактор синтеза Фишера-Тропша с подвижным слоем (16) находится в рабочем режиме, извлечение части (50) катализатора синтеза Фишера-Тропша из реактора (16) синтеза Фишера-Тропша с подвижным слоем, добавление реактивированного катализатора (57, 58) синтеза Фишера-Тропша в реактор (16) синтеза Фишера-Тропша с подвижным слоем и добавление свежего катализатора (60, 58) синтеза Фишера-Тропша в дополнение к реактивированному катализатору (57, 58) в реактор (16) синтеза Фишера-Тропша с подвижным слоем.

METHODS FOR CONVERSION OF METHANE IN SYNTHESIS GAS-

Regeneration method of poisoned catalyst containing ruthenium or ruthenium compound

内燃机的排气净化系统和方法

... 提供了一种用于内燃发动机(1)的排气净化系统，其包括NOx捕集型催化剂(13)和空/燃比控制器(20)，该空/燃比控制器(20)用于控制排气净化系统以使当是净化NOx捕集型催化剂捕集的NOx时，在预混合燃烧模式下，排气空/燃比变浓和NOx捕集型催化剂被激活(S13)，和使当是净化NOx捕集型催化剂的捕集的NOx时，在扩散燃烧模式下，排气空/燃比变浓和NOx捕集型催化剂不被激活(S15)。也提供一种排气净化方法。 ...

Processes and systems for producing syngas from methane

Embodiments of a process for producing syngas comprising hydrogen and carbon monoxide from a gas stream comprising methane are provided. The process comprises the step of contacting the gas stream with a two-component catalyst system comprising an apatite component and a perovskite component at reaction conditions effective to convert the methane to the syngas.

Process for the regeneration of hydrocarbon conversion catalysts

The present invention provides a process for hydrocarbon conversion, especially for producing aromatic hydrocarbons, which comprises: (a) alternately contacting a hydrocarbon feed, especially a lower alkane feed, with a hydrocarbon conversion catalyst, especially an aromatization catalyst, under hydrocarbon conversion, especially aromatization reaction conditions, in a reactor for a short period of time, preferably 30 minutes or less, to produce reaction products and then contacting the catalyst with hydrogen-containing gas at elevated temperature for a short period of time, preferably 10 minutes or less, (b) repeating the cycle of step (a) at least one time, (c) regenerating the catalyst by contacting it with an oxygen-containing gas at elevated temperature and (d) repeating steps (a) through (c) at least one time.

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.

PROCESS FOR REGENERATING CATALYST

Disclosed is a catalyst distributor and process for mixing spent catalyst and recycled regenerated catalyst in a regenerator vessel. Mixing is conducted in a confined space to which catalyst is delivered from catalyst conduits protruding through the wall of the regenerator. 1. A process for regenerating catalyst comprising:mixing spent catalyst having coke deposits and regenerated catalyst in a confined volume in a regenerator vessel to raise the temperature of the spent catalyst;allowing mixed catalyst to exit from the confined volume;distributing oxygen to a regenerator vessel;contacting said oxygen with said mixed catalyst to combust coke deposits from said spent catalyst in said mixed catalyst to produce regenerated catalyst and flue gas;separating said flue gas from said regenerated catalyst; andrecycling regenerated catalyst to said confined volume in said regenerator vessel.2. The process of wherein said spent catalyst and said regenerated catalyst are mixed in a cup defining said confined volume.3. The process of wherein said contacting of said oxygen with said spent catalyst is conducted in a first chamber and further comprising transporting said regenerated catalyst and flue gas from said first chamber into a second chamber and said separation of regenerated catalyst and flue gas is conducted in said second chamber.4. The process of wherein said regenerated catalyst from second chamber is recycled to a cup in said first chamber.5. The process of wherein mixed regenerated and spent catalyst exits from said confined volume downwardly.6. The process of further comprising propelling regenerated catalyst to said confined volume with transport gas.7. The process of wherein a recycled catalyst conduit delivers regenerated catalyst to said confined volume and a spent catalyst conduit delivers spent catalyst to said confined volume. This application is a Continuation of copending application Ser. No. 12/894,869 filed Sep. 30, 2010, the contents of which are hereby ...

CATALYST AND HYDROCARBON CONVERSION PROCESS UTILIZING THE CATALYST

The present invention relates to a hydrocarbon conversion catalyst comprising i) a catalyst, in oxidic form, metals M1, M2, M3 and M4, wherein: M1 is selected from Si, Al, Zr, and mixtures thereof; M2 is selected from Pt, Cr, and mixtures thereof; M3 is selected from W, Mo, Re and mixtures thereof; M4 is selected from Sn, K, Y, Yb and mixtures thereof; and ii) a hydrogen scavenger selected from at least one alkali and/or alkaline earth metal derivative, preferably in metallic, hydride, salt, complex or alloy form; as well as a hydrocarbon conversion process utilizing this catalyst. 1. Hydrocarbon conversion catalyst comprising , M1 is selected from Si, Al, Zr, and mixtures thereof;', 'M2 is selected from Pt, Cr, and mixtures thereof;', 'M3 is selected from W, Mo, Re and mixtures thereof;', 'M4 is selected from Sn, K, Y, Yb, and mixtures thereof; wherein', 'the mass fraction of M1 is in the range of 0.1 to 0.8;', 'the mass fraction of M2 is in the range of 0.001 to 0.2;', 'the mass fraction of M3 is in the range of 0.001 to 0.2;', 'the mass fraction of M4 is in the range of 0.0001 to 0.2; and', 'the mass fraction of oxygen is in the range of 0.1 to 0.8;', 'and, 'i) a catalyst in oxidic form, comprising metals M1, M2, M3 and M4, whereinii) a hydrogen scavenger selected from at least one alkali and/or alkaline earth metal derivative.2. Hydrocarbon conversion catalyst according to claim 1 , wherein the at least one alkali and/or alkaline earth metal is selected from Li claim 1 , Na claim 1 , K claim 1 , Mg claim 1 , Ca claim 1 , and mixtures thereof.3. Hydrocarbon conversion catalyst according to claim 1 , wherein weight ratio of catalyst i) and hydrogen scavenger ii) is from 1-99 to 99-1.4. Hydrocarbon conversion catalyst according to claim 1 , wherein M2 is Pt and M3 is W.5. Process for conversion of a hydrocarbon feed comprising saturated hydrocarbon compounds to olefin products comprising contacting a hydrocarbon feed stream with the hydrocarbon conversion catalyst ...

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 , ...

SEALING SYSTEM FOR A FLUID CATALYST CRACKING REGENERATOR

A regenerator for an FCC apparatus. The regenerator includes a riser inside of a shell. The riser includes a cone and a cone skirt. An annulus is formed between the riser and the shell. A sealing system for keeping catalyst out of a portion of the annulus comprises a first sealing element and a second sealing element disposed above the second sealing element. The second sealing element comprises a ring having one or more plates being movable to accommodate the thermal expansion of the riser. 1. A regenerator for regenerating catalyst from an FCC reactor , the regenerator comprising:an internal riser comprising a cone and a cone skirt,a shell surrounding the internal riser and forming an annulus between an outer surface of the riser and an inner surface of the shell, a bottom of the cone skirt being secured to the shell;a primary seal disposed in the annulus between the internal riser and the shell; and,a secondary seal disposed above the primary seal, wherein the secondary seal comprises a sealing ring including at least one pivotable plate.2. The regenerator of claim I wherein the sealing ring forms a cone.3. The regenerator of claim I wherein the sealing ring forms a plate4. The regenerator of claim I wherein the secondary seal further comprises an outer seal support ring secured to the inner surface of the shell , the outer seal support ring forming a lap joint with the at least one pivotable plate.5. The regenerator of wherein the secondary seal further comprises an inner seal support ring secured to the outer surface of the riser.6. The regenerator of claim 5 , wherein the inner seal support ring comprises at least one post.7. The regenerator of claim 6 , wherein the at least one pivotable plate includes an aperture to receive the at least one post claim 6 , and wherein the at least one post forms a pivot for the at least one pivotable plate.8. The regenerator of wherein the inner seal support ring includes plurality of posts claim 7 , and wherein the secondary ...

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 the regeneration of a titanium zeolite catalyst for propylene epoxidation

The invention relates to process for the regeneration of a catalyst comprising a titanium containing zeolite as catalytically active material comprising a stage comprising introducing a feed stream comprising propene, hydrogen peroxide or a hydrogen peroxide source, and an organic solvent into a reactor containing a catalyst comprising the titanium containing zeolite, subjecting the feed stream in the reactor to epoxidation conditions in the presence of the catalyst, removing a product steam comprising propylene oxide and the organic solvent from the reactor, stopping introducing the feed stream, washing the catalyst with a liquid aqueous system and calcining the washed catalyst.

UNSATURATED HYDROCARBON PRODUCTION METHOD AND DEHYDROGENATION CATALYST REGENERATION METHOD

A method for producing an unsaturated hydrocarbon comprising: a dehydrogenation step of contacting a raw material gas containing at least one hydrocarbon selected from a group consisting of alkanes and olefins with a dehydrogenation catalyst containing a group 14 metal element and Pt to obtain a product gas containing at least one unsaturated hydrocarbon selected from the group consisting of olefins and conjugated dienes, and a regeneration step of contacting the dehydrogenation catalyst subjected to the dehydrogenation step with a regenerating gas containing molecular oxygen under a temperature condition of 310 to 450° C. 1. A method for producing an unsaturated hydrocarbon comprising:a dehydrogenation step of contacting a raw material gas containing at least one hydrocarbon selected from a group consisting of alkanes and olefins with a dehydrogenation catalyst containing a group 14 metal element and Pt to obtain a product gas containing at least one unsaturated hydrocarbon selected from a group consisting of olefins and conjugated dienes, anda regeneration step of contacting the dehydrogenation catalyst subjected to the dehydrogenation step with a regenerating gas containing molecular oxygen under a temperature condition of 310 to 450° C.2. The method according to claim 1 , wherein the group 14 metal element includes Sn.3. The method according to claim 1 , wherein the dehydrogenation catalyst is a catalyst in which a group 14 metal element and Pt are supported on a carrier using a metal source containing no chlorine atom.4. The method according to claim 1 , wherein the raw material gas contains an alkane having 2 to 10 carbon atoms.5. The method according to claim 1 , wherein the raw material gas contains an olefin having 4 to 10 carbon atoms.6. A method of regenerating a dehydrogenation catalyst containing a group 14 metal element and Pt that has been used for a dehydrogenation reaction of a hydrocarbon claim 1 , the method comprising:a regeneration step of ...

Methods of Regenerating Aromatization Catalysts

Methods for treating or rejuvenating a spent catalyst are disclosed. Such methods can employ a step of halogenating the spent catalyst, followed by decoking the halogenated spent catalyst. The halogenation step can utilize fluorine and chlorine together, or fluorine and chlorine can be applied sequentially. 120-. (canceled)21. A method of treating a spent catalyst comprising platinum and a catalyst support , the method comprising:(i) contacting the spent catalyst with a pre-drying gas stream consisting essentially of an inert gas;(ii) contacting the spent catalyst with a chlorine-containing stream comprising a chlorine-containing compound to produce a chlorinated spent catalyst;(iii) contacting the chlorinated spent catalyst with a fluorine-containing stream comprising a fluorine-containing compound to produce a chlorinated-fluorinated spent catalyst;(iv) contacting the chlorinated-fluorinated spent catalyst with a purging stream consisting essentially of an inert gas; and(v) contacting the chlorinated-fluorinated spent catalyst with a decoking gas stream comprising oxygen to produce a de-coked catalyst.22. The method of claim 21 , wherein the spent catalyst comprises from about 0.1 wt. % to about 10 wt. % platinum.23. The method of claim 22 , wherein the spent catalyst comprises:from about 0.5 to about 2 wt. % platinum;from about 0.025 wt. % to about 5 wt. % chlorine;from about 0.025 wt. % to about 5 wt. % fluorine; anda catalyst support comprising a bound medium and/or large pore zeolite and a support matrix.24. The method of claim 22 , wherein the pre-drying gas stream consists essentially of nitrogen.25. The method of claim 22 , wherein:step (ii) is conducted at a chlorination temperature in a range from about 25° C. to about 250° C.;a concentration of chlorine (Cl) in the chlorine-containing stream is in a range from about 50 to about 25,000 ppm by volume; and{'sub': '2', 'the chlorine-containing stream comprises Cland nitrogen, and is substantially free of ...

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 ...

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 ...

CATALYST REGENERATORS AND METHODS FOR REGENERATING CATALYSTS

Catalyst regenerators and methods of their use are provided. A catalyst regenerator includes a combustion chamber with a combustion chamber diameter and a combustion chamber bottom. A mixing chamber is fluidly coupled to the combustion chamber at the combustion chamber bottom, where the mixing chamber has an exterior wall and a mixing chamber diameter less than the combustion chamber diameter. A first and second catalyst inlet are fluidly coupled to the mixing chamber, and a mixing cylinder is within the mixing chamber. The mixing cylinder and the exterior wall define an annular space there-between, and the mixing cylinder includes a cylinder opening. 1. A catalyst regenerator comprising:a combustion chamber having a combustion chamber diameter and a combustion chamber bottom;a mixing chamber fluidly coupled to the combustion chamber at the combustion chamber bottom, wherein the mixing chamber has an exterior wall and a mixing chamber diameter less than the combustion chamber diameter;a first catalyst inlet fluidly coupled to the mixing chamber;a second catalyst inlet fluidly coupled to the mixing chamber; anda mixing cylinder within the mixing chamber, wherein the mixing cylinder and the exterior wall define an annular space there-between, and wherein the mixing cylinder comprises a cylinder opening.2. The catalyst regenerator of wherein the cylinder opening extends from below a lower most portion of the first catalyst inlet to above an upper most portion of the first catalyst inlet.3. The catalyst regenerator of wherein the mixing cylinder comprises a cylinder top that is closed claim 1 , and wherein the cylinder opening terminates below the cylinder top.4. The catalyst regenerator of wherein the mixing cylinder comprises a cylinder wall section claim 1 , and wherein the cylinder wall section is positioned facing the first catalyst inlet and the second catalyst inlet.5. The catalyst regenerator of wherein the cylinder opening faces one of the first catalyst inlet ...

Apparatuses and methods for cooling catalyst

Apparatuses and methods for cooling catalyst are provided. In one embodiment, an apparatus for cooling catalyst includes a catalyst cooler vessel having a catalyst inlet for receiving catalyst. The apparatus includes a gas distributor lance positioned in the catalyst cooler vessel and having a gas outlet configured for injecting gas into the catalyst. The apparatus also includes a heat exchange tube positioned in the catalyst cooler vessel and having an outer surface. The heat exchange tube is configured to transfer heat from the catalyst to a heat exchange fluid. The apparatus further includes a hard surfacing material located on the outer surface of the heat exchange tube.

USE OF A FUEL OIL WASH TO REMOVE CATALYST FROM A FLUIDIZED-BED PROPANE DEHYDROGENATION REACTOR EFFLUENT

A process where external fuel oil is used to wash entrained catalyst from a fluidized-bed propane dehydrogenation reactor effluent, where the fuel oil and catalyst mixture is returned to the reactor to provide the net fuel required for catalyst regeneration. Optionally the fluidized-bed propane dehydrogenation reactor effluent and the fuel oil are contacted in a direct contact inline device before entering a flash zone in the reactor vessel. 1. A method for recovering catalyst from a fluidized-bed propane dehydrogenation reactor effluent gas , the method comprising:(a) cooling fluidized-bed propane dehydrogenation reactor effluent gas;(b) contacting the cooled effluent gas with fuel oil in a wash section to wash out catalyst to obtain a cooled effluent gas essentially free of catalyst;(c) withdrawing an oil-catalyst slurry from the wash section and circulating the oil-catalyst slurry through a filter thereby removing catalyst from the fuel oil giving filtered wash oil;(d) returning filtered wash oil to the wash section as recirculated wash oil; and(e) backwashing the filter thereby recovering catalyst.2. The method of where the contacting and returning steps are effected in a quench tower comprising vapor-liquid contact elements and a bottoms zone holding a fuel oil inventory.3. The method of further comprising cooling the recirculated wash oil before the contacting step.4. The method of where circulating the oil-catalyst slurry through a filter comprises continuously passing the oil-catalyst slurry through at least one first filter in a filtration mode to separate the catalyst therefrom giving filtrate while at least one second filter in parallel with the first filter is in a backwashing mode thereby removing the separated catalyst therefrom.5. The method of further comprising returning filtrate from the first filter to the fuel oil inventory.6. The method of where the backwashing of the at least one filter further comprises periodically alternating the at least ...

A CATALYTIC PROCESS FOR CO-PRODUCTION OF BENZENE, ETHYLENE, AND HYDROGEN

A process for the production of benzene and ethylene from an alkane-containing gas stream. The alkane-containing gas stream may be contacted, in a reaction zone of a reactor under alkane aromatization conditions, with an aromatization catalyst including any combination of fresh, spent, and regenerated catalyst to produce an outlet stream including (i) spent catalyst and (ii) a product mixture including benzene and ethylene. The spent catalyst may be regenerated in a regeneration zone under regeneration conditions to produce the regenerated catalyst. A selected amount of fresh catalyst may be added to the regeneration zone to produce the mixture of fresh catalyst and regenerated catalyst, which may be recycled to the reaction zone. A ratio of benzene to ethylene in the product mixture may be controlled by modifying the alkane aromatization conditions, the regeneration conditions, and/or the selected amount of fresh catalyst added to the regeneration zone. 1. A process for the production of benzene and ethylene from an alkane-containing gas stream , which alkane-containing gas stream contains at least one alkane selected from the group consisting of ethane , propane or butane , comprising:(a) contacting the alkane-containing gas stream, in a reaction zone of a reactor under alkane aromatization conditions, with an aromatization catalyst comprising a mixture of fresh catalyst and regenerated catalyst to produce an outlet stream comprising (i) spent catalyst and (ii) a product mixture comprising benzene and ethylene,(b) separating the spent catalyst from the product mixture in the outlet stream,(c) regenerating the separated spent catalyst in a regeneration zone under regeneration conditions to produce the regenerated catalyst,(d) adding a selected amount of fresh catalyst to the regeneration zone to produce the mixture of fresh catalyst and regenerated catalyst,(e) recycling the mixture of fresh catalyst and regenerated catalyst to the reaction zone, and(f) controlling ...

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 REGENERATING A COKED CATALYTIC CRACKING CATALYST

A process for regenerating a coked catalytic cracking catalyst which the carbon-containing deposits on the catalyst contains at least 1 wt % bio-carbon, based on the total weight of carbon present in the carbon-containing deposits is provided. Such coked catalytic cracking catalyst is contacted with an oxygen containing gas at a temperature of equal to or more than 550° C. in a regenerator to produce a regenerated catalytic cracking catalyst, heat and carbon dioxide. 1. A process for regenerating a coked catalytic cracking catalyst , comprising contacting the coked catalytic cracking catalyst with an oxygen containing gas at a temperature of equal to or more than 550° C. in a regenerator to produce a regenerated catalytic cracking catalyst , heat and carbon dioxide , wherein the coked catalytic cracking catalyst comprises carbon-containing deposits , which carbon-containing deposits comprise at least 1 wt % bio-carbon , based on the total weight of carbon present in the carbon-containing deposits.2. The process of wherein the oxygen-containing gas comprises more than 21 vol. % oxygen claim 1 , based on the total volume of the oxygen-containing gas.3. The process of wherein the coked catalytic cracking catalyst is produced by contacting a solid biomass material with a catalytic cracking catalyst at a temperature of more than 400° C. in a catalytic cracking reactor.4. The process of wherein the coked catalytic cracking catalyst is produced by contacting the biomass material and a fluid hydrocarbon feed with a catalytic cracking catalyst at a temperature of equal to or more than 400° C. in a catalytic cracking reactor claim 1 , wherein the catalytic cracking reactor is a riser reactor and the biomass material is supplied to the riser reactor upstream of the fluid hydrocarbon feed.5. The process of wherein the biomass material is a solid biomass material.6. The process of wherein the coked catalytic cracking catalyst is contacted with the oxygen containing gas in the ...

Method of reactivating catalyst

Systems and methods for using and regenerating a catalyst for producing acetic acid from ethane are disclosed. Feed stream comprising ethane and an oxidant including oxygen is flowed to a reactor, in which a catalyst comprising MoVNbPd oxide is disposed. The ethane and the oxidant are reacted in presence of the catalyst under reaction conditions sufficient to produce acetic acid. When the catalyst's ability to catalyze the reaction between the ethane and the oxidant is reduced by a predetermined percentage, the flow of the feed stream to the reactor is ceased. A regenerating gas stream is flowed through the reactor to contact the regenerating gas stream with the catalyst under operating conditions to increase the catalyst's ability to catalyze the reaction between the ethane and the oxidant.

PROCESS FOR OPERATING A HIGHLY PRODUCTIVE TUBULAR REACTOR

The present technology is directed to processes for conversion of synthesis gas in a tubular reactor to produce a synthetic product that utilizes high activity carbon monoxide hydrogenation catalysts and a heat transfer structure that surprisingly provides for higher per pass conversion with high selectivity for the desired synthetic product without thermal runaway. 114-. (canceled)15. A tubular reactor comprising:one or more reactor tubes including a tube inlet;a tube outlet located downstream of the tube inlet;an inner tube wall defining an interior of the one or more reactor tubes;an outer tube wall defining an exterior of the one or more reactor tubes;a volume of a catalyst provided in at least one section within the interior of the one or more reactor tubes; anda heat transfer structure provided within the interior of the one or more reactor tubes, the heat transfer structure being in conductive thermal contact with a portion of the catalyst and in at least partial conductive thermal contact with the inner tube wall throughout a surface area of the inner tube wall in the at least one section containing the catalyst;a reactor inlet in fluid communication with the one or more reactor tubes; anda reactor outlet located downstream of the reactor inlet and in fluid communication with the one or more reactor tubes,wherein the tubular reactor satisfies at least one of the following conditions:{'sub': eff', 'cat, 'a ratio of an effective thermal conductivity of the heat transfer structure and the catalyst with the inner tube wall to a thermal conductivity of the catalyst (k/k) is at least 50:1, or'}{'sup': 2', '3', '2', '3, 'a total combined surf ace area of the heat transfer structure and inner tube wall containing the catalyst per volume of the catalyst (the “SA/V”) is about 500 m/mto about 4000 m/m.'}16. The tubular reactor of claim 15 , wherein at least about 5% of the surface area of the inner tube wall containing the carbon monoxide hydrogenation catalyst is in ...

Mixed Metal Oxide Catalyst useful for Paraffin Dehydrogenation

The invention relates to a catalyst composition suitable for the dehydrogenation of paraffins having 2-8 carbon atoms comprising zinc oxide and titanium dioxide, optionally further comprising oxides of cerium (Ce), dysprosium (Dy), erbium (Er), europium (Eu), gadolinium (Gd), lanthanum (La), neodymium (Nd), praseodymium (Pr), samarium (Sm), terbium (Tb), ytterbium (Yb), yttrium (Y), tungsten (W) and Zirconium (Zr) or mixtures thereof, wherein said catalyst composition is substantially free of chromium and platinum. The catalysts possess unique combinations of activity, selectivity, and stability. Methods for preparing improved dehydrogenation catalysts and a process for dehydrogenating paraffins having 2-8 carbon atoms, comprising contacting the mixed metal oxide catalyst with paraffins are also described. The catalyst may also be disposed on a porous support in an attrition-resistant form and used in a fluidized bed reactor. 133-. (canceled)34. A process for continuous dehydrogenating of paraffins having 2-8 carbon atoms , preferably propane or isobutane , comprising:{'sup': −1', '−1, 'contacting said paraffins with a catalyst composition at a reaction temperature of 500-800° C., a space velocity of 0.1-5 hror 0.1-1 hrand a pressure of 0.01-0.2 MPa for a reaction period in the range of 0.05 seconds to 10 minutes;'}regenerating the catalyst with an oxygen-containing gas wherein said catalyst regeneration is performed at a reaction temperature of 500-800° C., a pressure of 0.01-0.2 MPa and a regeneration period ranging from 0.05 seconds to 10 minutes;wherein the catalyst composition comprises:(a) zinc oxide with optional modifiers selected from the group of Copper, Manganese, and Niobium and a stabilized titania support, comprising: the stabilized titania support stabilized with a stabilizing element(s) comprising zirconium, tungsten, or a rare earth element or combinations thereof; and Zn; wherein the catalyst composition from 10 to 95 wt % titania, 0.1 to 25 wt % ...

CATALYST REGENERATING METHODS AND APPARATUSES AND METHODS OF INHIBITING CORROSION IN CATALYST REGENERATING APPARATUSES

Methods and apparatuses for regenerating catalysts and methods of inhibiting corrosion in catalyst regenerating apparatuses are provided. An exemplary apparatus includes: a metal vessel configured to receive a spent catalyst stream and contact at least a portion of the spent catalyst stream with an oxygen containing environment at a sufficiently high temperature to burn coke present in the spent catalyst stream; a refractory material overlying at least a portion of an inner surface of the metal vessel; and a corrosion inhibiting material in contact with at least a portion of the inner surface of the metal vessel and disposed between the inner surface and at least a portion of the refractory material, wherein the corrosion inhibiting material is heat stable at a temperature of at least up to about 400° F. (about 204° C.) and inhibits contact of an acid environment with the inner surface of the metal vessel. 1. A catalyst regenerating apparatus comprising:a metal vessel having an inner surface and configured to receive a spent catalyst stream and an oxygen-containing gas, and to provide an oxygen containing environment at a sufficiently high temperature to burn coke present on the spent catalyst stream and generate regenerated catalyst, wherein the spent catalyst stream comprises catalyst having coke deposits;a refractory material overlying at least a portion of the inner surface of the metal vessel; anda corrosion inhibiting material overlying at least a portion of the inner surface of the metal vessel and disposed between the inner surface and at least a portion of the refractory material, wherein the corrosion inhibiting material is heat stable at a temperature of at least up to about 400° F. (about 204° C.) and inhibits contact of an acid environment with the inner surface of the metal vessel.2. The catalyst regenerating apparatus of claim 1 , wherein at least a region of the metal vessel is configured to receive and accumulate regenerated catalyst.3. The catalyst ...

A process for the dehydrogenation of alkanes to alkenes and iron-based catalysts for use in the process

In a process for the catalytic dehydrogenation of lower alkanes to the corresponding alkenes, a regenerable catalyst comprising iron carbide supported on a carrier is used. A small amount (below 100 ppm) of a sulfur compound, such as H2S, is added during the process.

SYSTEMS AND METHODS FOR CATALYTIC UPGRADING OF VACUUM RESIDUE TO DISTILLATE FRACTIONS AND OLEFINS

Systems and methods for upgrading a heavy oil feed to a light product comprising distillate fractions and olefins, the method including combining a heavy oil feed with a naphtha-based cracking additive to produce a mixed heavy oil feed; heating the mixed heavy oil feed with a nano-zeolite catalyst to effect catalytic upgrading of the mixed heavy oil feed to produce lighter distillate fractions and olefins in an upgraded product; and separating the lighter distillate fractions from the olefins. 1. A method for upgrading a heavy oil feed to a light product comprising distillate fractions and olefins , the method comprising the steps of:combining a heavy oil feed with a naphtha-based cracking additive to produce a mixed heavy oil feed;heating the mixed heavy oil feed with a nano-zeolite catalyst, where the step of heating is carried out without hydrogen addition and without steam addition, to effect catalytic upgrading of the mixed heavy oil feed to produce lighter distillate fractions and olefins in an upgraded product, the upgraded product including at least about 20 wt. % olefins; andseparating the lighter distillate fractions from the olefins, where the nano-zeolite catalyst to mixed heavy oil feed weight ratio is between about 0.5:2 to about 0.5:24.2. The method according to claim 1 , where the heavy oil feed has an American Petroleum Institute (API) gravity between about 5 and about 22.3. The method according to claim 1 , where the heavy oil feed is selected from the group consisting of: de-asphalted oil claim 1 , de-metalized oil claim 1 , heavy vacuum gas oil claim 1 , and combinations thereof.4. The method according to claim 1 , where the naphtha-based cracking additive comprises straight run naphtha with an API gravity from about 40 to about 77 and a boiling point range from between about 200° F. to 500° F.5. The method according to claim 1 , where the naphtha-based cracking additive includes at least one component selected from the group consisting of: ...

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 ...

HYDROGEN SULFIDE REMOVAL PROCESS

A process is presented to treat a process stream containing a hydrocarbon (oil and/or gas) and hydrogen sulfide with a liquid treatment solution containing a sulfur dye catalyst. The process stream can be within a pipeline, wellbore, subsea pipeline or a wellhead that contains hydrogen sulfide where the liquid treatment solution is injected at a predetermined point to define a scavenger zone such that the sulfur dye catalyst in the liquid treatment solution causes the sulfide from the hydrogen sulfide to react with the catalyst. The hydrocarbon component is separated substantially free of the hydrogen sulfide from a spent treatment solution containing spent sulfur dye catalyst which can then be fed to an oxidation vessel where it is contacted with an oxygen containing gas causing the sulfide to oxidize to thiosulfate and converting the spent sulfur dye catalyst to regenerated sulfur dye catalyst. The thiosulfate can be recovered, and the regenerated sulfur dye catalyst can be recycled as part of the liquid treatment solution. 1. A process to treat hydrogen sulfide in a subsea pipeline comprising:injecting a liquid treatment solution comprising a sulfur dye catalyst into a subsea pipeline containing a hydrocarbon and hydrogen sulfide to form an admixture, where the point of injection of the liquid treatment solution into the subsea pipeline is selected at a distance below sea level to define a scavenger region within the pipeline such that the hydrogen sulfide is absorbed into the liquid treatment solution and reacts to form a spent sulfur dye catalyst; anddirecting the admixture into a separator where treated hydrocarbon and dissolved gas is separated from a spent treatment solution comprising the spent sulfur dye catalyst and water.2. The process of further comprising claim 1 ,introducing the spent treatment solution into an oxidation vessel;introducing an oxygen containing gas into the oxidation vessel to contact the spent treatment solution causing the sulfide ...

Molybdenum-vanadium bimetallic oxide catalyst and its application in chemical looping oxidative dehydrogenation of alkane

A molybdenum-vanadium bimetallic oxide catalyst and its application in the chemical looping oxidative dehydrogenation of alkane. The molecular formula of molybdenum-vanadium bimetallic oxide catalyst is MoVy and y represents the atomic molar ratio of vanadium and molybdenum. The supported MoVy catalyst is prepared by impregnation method, following the drying, calcination and tablet pressing. The reaction temperature was 450-550° C., and propane could be oxidized and dehydrogenated to propylene with high activity and selectivity, with propane conversion rate remaining at 30-40% and propylene selectivity at 80-90%. The fresh catalysts were reduced to the lower valence states with the lattice oxygen diffusion to propane. After the dehydrogenation, the reduced samples were regenerated to recover to the initial state and regain the lattice oxygen. During the redox cycles, the reaction performance remains stable, which can be used in the fixed bed reactor, moving bed reactor or circulating fluidized bed.

PROCESSES FOR REGENERATING CATALYSTS USEFUL IN FISCHER-TROPSCH PROCESSES

The present disclosure relates to processes for regenerating catalysts. In certain aspects, a process for regenerating a deactivated catalyst disposed in a first organic material includes removing a substantial portion of the first organic material from the catalyst to provide a dewaxed catalyst having less than about 40 wt % (e.g., less than about 20%) organic material disposed thereon. The dewaxed catalyst is then contacted with a flow of a substantially inert gas at a temperature of at least about 200° C. to provide an inert gas-treated catalyst having less than about 10 wt % organic material disposed thereon. The inert gas-treated catalyst is then contacted with an oxygen-containing gas at a temperature of at least about 200 ° C. to form an oxidized catalyst (e.g., having less than 2 wt % carbonaceous material disposed thereon). The oxidized catalyst is then contacted with a hydrogen-containing gas at a temperature of at least about 200° C. to form a regenerated catalyst. Finally, the regenerated catalyst can be disposed in a second organic material. The regenerated catalysts can be useful, for example, in Fischer-Tropsch processes. 1. A process for regenerating a deactivated catalyst , the catalyst being disposed in a first organic material , the catalyst comprising a catalytic metal disposed on a support , the process comprisingremoving a substantial portion of the first organic material from the catalyst to provide a dewaxed catalyst having less than about 40 wt % organic material disposed thereon;contacting the dewaxed catalyst with a flow of a substantially inert gas at a temperature of at least about 200° C. to provide an inert gas-treated catalyst having less than about 10 wt % organic material disposed thereon;contacting the inert gas-treated catalyst with an oxygen-containing gas at a temperature of at least about 200° C., the contacting being performed to substantially remove any residual carbonaceous material remaining disposed on the dewaxed catalyst ...

EXHAUST PURIFIER

The purpose of the present invention is to provide an exhaust purifier which suppresses unnecessary consumption of pressurization air so as to improve a removal rate of dust. An exhaust purifier for removing particulate matter adhered to a NOx catalyst by injecting pressurized air using an air injection nozzle into a housing of a catalyst reactor in which the NOx catalyst serving as a catalyst is positioned, wherein an injection valve of a soot blower supplying pressurized air into the housing of the catalyst reactor is opened and closed based on an exhaust gas flow rate so as to inject the pressurized air. 1. An exhaust purifier wherein compressed air is injected into a catalyst reactor in which a catalyst is arranged based on an exhaust gas flow rate so as to remove dust adhering to the catalyst ,characterized in thatwhen the exhaust gas flow rate is not more than a reference exhaust gas flow rate, the compressed air is injected into the catalyst reactor at a predetermined condition.2. The exhaust purifier according to claim 1 , wherein when a pressure difference between exhaust gas upstream the catalyst and exhaust gas downstream thereof is raised higher than a pressure difference between exhaust gas upstream the catalyst and exhaust gas downstream thereof at an initial state at the same exhaust flow rate for not less than a reference pressure difference raising amount claim 1 , the compressed air is injected into the catalyst reactor at a condition different from the predetermined condition regardless of the exhaust gas flow rate. The present invention relates to an exhaust purifier of an internal combustion engine.Conventionally, an exhaust purifier which reduces NOx to nitrogen and water with a catalyst reactor in which a selective reduction NOx catalyst (SCR catalyst) is arranged and ammonia which is a reducing agent so as to decrease NOx (nitrogen oxide) included in exhaust gas from an internal combustion engine is known. The ammonia is generated by urea ...

EXHAUST PURIFIER

The purpose of the present invention is to provide an exhaust purifier () which is capable of restoring a pressure difference (ΔP) and a purification rate (NOx removal efficiency) of a NOx catalyst () to the initial states thereof. An exhaust purifier () for removing particulate matter adhered to a NOx catalyst () by injecting pressurized air using an air injection nozzle () into a housing () of a catalyst reactor () in Which the NOx catalyst () serving as a catalyst is positioned, wherein the particulate matter is removed by increasing the pressure inside the catalyst reactor () to a prescribed pressure (ΔIP) within a prescribed interval of time (t) by operating an injection valve () for supplying pressurized air 1. An exhaust purifier wherein compressed air is injected into a catalyst reactor in which a catalyst is arranged so as to remove dust adhering to the catalyst ,characterized in thatby operating an injection valve supplying the compressed air, pressure in the catalyst reactor is raised to predetermined pressure within predetermined time so as to remove the dust.2. The exhaust purifier according to claim 1 , wherein a shock wave is generated in the catalyst reactor by the compressed air so as to remove the dust.3. The exhaust purifier according to claim 1 , wherein an injection port of an air injection nozzle injecting the compressed air is arranged near a wall surface of the catalyst reactor.4. The exhaust purifier according to claim 2 , wherein an injection port of an air injection nozzle injecting the compressed air is arranged near a wall surface of the catalyst reactor. The present invention relates to an exhaust purifier of an internal combustion engine.Conventionally, an exhaust purifier which reduces NOx to nitrogen and water with a catalyst reactor in which a selective reduction NOx catalyst (SCR catalyst) is arranged and ammonia which is a reducing agent so as to decrease NOx (nitrogen oxide) included in exhaust gas from an internal combustion ...

Furan-2,5-dicarboxylic acid purge process

Disclosed is an oxidation process to produce a crude carboxylic acid product carboxylic acid product. The process comprises oxidizing a feed stream comprising at least one oxidizable compound to generate a crude carboxylic acid slurry comprising furan-2,5-dicarboxylic acid (FDCA) and compositions thereof. Also disclosed is a process to produce a dry purified carboxylic acid product by utilizing various purification methods on the crude carboxylic acid.

CATALYST COOLER FOR REGENERATED CATALYST

A catalyst cooler for cooling regenerated catalyst in a regenerator associated with a fluid catalytic cracking unit. The catalyst cooler includes a first passage for transporting hot regenerated catalyst away from the regenerator and a second passage for returning cooled regenerated catalyst to the regenerator. The catalyst cooler also includes at least one heat exchanger. The second passage may be disposed within the first passage, or the first and second passage may each occupy a portion of a horizontal cross section of the catalyst cooler. 1. A regenerator for regenerating spent catalyst particles , the regenerator comprising:an inlet for spent catalyst particles;an outlet for regenerated catalyst particles;a gas distributor disposed below a bed of catalyst particles configured to supply combustion gas into the regenerator for combusting coke on the spent catalyst particles to provide the regenerated catalyst particles; and,a cooling zone for removing heat from regenerated catalyst, the cooling zone comprising a first passage for receiving regenerated catalyst, a second passage for returning cooled regenerated catalyst to the regenerator, and at least one heat exchanger for removing heat from the regenerated catalyst, wherein each heat exchanger in the cooling zone is disposed in at least one of the first passage and the second passage.2. The regenerator of wherein the first passage comprises a conduit disposed within the second passage.3. The regenerator of wherein the second passage comprises a conduit disposed within the first passage.4. The regenerator of wherein the first passage and the second passage each comprise a portion of a single shell.5. The regenerator of wherein each heat exchanger includes a longitudinal axis claim 1 , and wherein the longitudinal axis of each heat exchanger is generally parallel to a flow path of the regenerated catalyst through the first passage.6. The regenerator of claim 1 , wherein the catalyst cooler further comprises an ...

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 ...

Methods for Regenerating Sulfur-Contaminated Aromatization Catalysts

Methods for regenerating a sulfur-contaminated catalyst are disclosed. Such methods may employ a step of washing the sulfur-contaminated catalyst with an aqueous solution containing an alkali metal, followed by contacting the washed catalyst with a halogen solution containing chlorine and fluorine. 1. A method for regenerating a sulfur-contaminated catalyst comprising a transition metal and a catalyst support , the method comprising:(1) washing the sulfur-contaminated catalyst with an aqueous solution, the aqueous solution optionally comprising an alkali metal, to produce a washed catalyst; and(2) contacting the washed catalyst with a halogen solution comprising chlorine and fluorine to produce a halogenated catalyst.2. The method of claim 1 , wherein the aqueous solution comprises the alkali metal.3. The method of claim 2 , wherein:the transition metal comprises platinum;the catalyst support comprises a KL-zeolite and a support matrix comprising alumina, silica, a mixed oxide thereof, or a mixture thereof; and from about 100 ppmw to about 1000 ppmw sulfur;', 'from about 0.05 wt. % to about 2 wt. % chlorine; and', 'from about 0.05 wt. % to about 2 wt. % fluorine., 'the sulfur-contaminated catalyst comprises4. The method of claim 3 , wherein the sulfur-contaminated catalyst contains less than about 0.1 wt. % of barium.5. The method of claim 1 , wherein the aqueous solution comprises a salt of potassium claim 1 , rubidium claim 1 , cesium claim 1 , or any combination thereof.6. The method of claim 1 , wherein:step (1) comprises from 2 to 8 washing cycles;each washing cycle is conducted independently at a washing temperature in a range from about 20° C. to about 95° C. and for a time period in a range from about 5 minutes to about 2 hours; andeach washing cycle is conducted independently with either an aqueous solution comprising the alkali metal or an aqueous solution that does not contain an alkali metal.7. The method of claim 6 , wherein a ratio of the weight of the ...

CATALYTIC GAS PHASE FLUORINATION

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

Honeycomb monolith structure loaded with nanozeolites for enhanced propylene selectivity in methanol conversion

A catalyst system and a process for methanol to light olefin conversion with enhanced selectivity towards propylene. The catalyst system comprises a honeycomb monolith catalyst support coated with aluminosilicate nanozeolite catalysts on the edges and inside the channels of the support structure. The aluminosilicate nanozeolite catalysts have not been pre-modified with a promoter metal. The catalyst system gives higher hydrothermal stability to the catalyst compared to randomly packed pellet catalysts and allows methanol to be converted to predominantly propylene at a low temperature, with decreased selectivity towards C 2 , higher olefins and paraffinic hydrocarbons.

PROCESS FOR PREPARING ETHYLENE AND/OR PROPYLENE

A process for preparing ethylene and/or propylene, wherein oxygenates and olefins are converted to ethylene and/or propylene over a zeolite-comprising catalyst, in two reaction steps. The catalyst is circulated in the reaction system. 1. A process for preparing ethylene and/or propylene , wherein oxygenates and olefins are converted to ethylene and/or propylene over a zeolite-comprising catalyst , comprising the steps of:a) reacting in a first reactor an oxygenate feed over the zeolite-comprising catalyst at a temperature in the range of from 350 to 1000° C. and retrieving from the first reactor a first reactor effluent stream comprising gaseous products, including ethylene and/or propylene, and zeolite-comprising catalyst;b) reacting in a second reactor an olefin feed over the zeolite-comprising catalyst at a temperature in the range of from 500 to 700° C. and retrieving from the second reactor a second reactor effluent stream comprising gaseous products, including ethylene and/or propylene, and zeolite-comprising catalyst;c) providing the first and second reactor effluent stream to one or more gas/solid separators to retrieve zeolite-comprising catalyst from the first and second reactor effluent;d) providing part of the zeolite-comprising catalyst retrieved in step (c) to the first reactor;e) regenerating another part of the zeolite-comprising catalyst retrieved in step (c) by contacting the zeolite-comprising catalyst with oxygen at elevated temperatures to provide a hot regenerated zeolite-comprising catalyst; andf) providing part of the hot regenerated zeolite-comprising catalyst to the first reactor and another part of the hot regenerated zeolite-comprising catalyst to the second reactor.2. A process according to claim 1 , wherein at least part of the first and second effluent are provided to the same gas/solid separator.3. A process according to claim 1 , wherein the first reactor and/or the second reactor is a riser reactor.4. A process according to claim 1 ...

CATALYST COMPOSITION AND REACTIVATION PROCESS USEFUL FOR ALKANE DEHYDROGENATIONS

A catalyst comprising a Group IIIA metal, a Group VIII noble metal, and an optional promoter metal, on a support selected from silica, alumina, silica-alumina compositions, rare earth modified alumina, and combinations thereof, doped with iron, a Group VIB metal, a Group VB metal, or a combination thereof, offers decreased reactivation time under air soak in comparison with otherwise identical catalysts. Reducing reactivation time may, in turn, reduce costs, both in inventory and capital. 1. An alkane dehydrogenation catalyst composition comprisinga Group IIIA metal selected from gallium, indium, thallium and combinations thereof;a Group VIII noble metal selected from platinum, palladium, rhodium, iridium, ruthenium, osmium, and combinations thereof;at least one dopant selected from iron, chromium, vanadium, and combinations thereof;and an optional promoter metal selected from sodium, potassium, rubidium, cesium, magnesium, calcium, strontium, barium and combinations thereof;on a catalyst support selected from silica, alumina, silica-alumina composites, rare earth modified alumina, and combinations thereof.2. The catalyst composition of whereinthe Group IIIA metal ranges from 0.25 percent by weight to 5 percent by weight;the Group VIII noble metal ranges from 5 parts by weight to 500 parts by weight;the optional promoter metal ranges from 0 percent by weight to 2.0 percent by weight; andthe dopant, where such dopant is iron, ranges from greater than 100 parts by weight to 2100 parts by weight,and where such dopant is chromium, vanadium, or a combination thereof, ranges from 100 parts by weight to 800 parts by weight, and combinations thereof;each percent by weight based upon weight of the total alkane dehydrogenation catalyst, andeach part by weight based upon one million parts by weight of the total alkane dehydrogenation catalyst.3. The catalyst composition of wherein at least one selection is made from: the alkane is propane; the Group VIII noble metal is ...

METHOD FOR REACTIVATING USED HYDROGENATION TREATMENT TITANIA CATALYST, AND REGENERATED HYDROGENATION TREATMENT TITANIA CATALYST

Provided is a method of reactivating a used titania catalyst for hydrogenation treatment, capable of improving the catalytic activity of the used titania catalyst for hydrogenation treatment that is obtained by supporting a catalyst component on a titania support and exhibits reduced catalytic activity after having been used for hydrogenation treatment of a hydrocarbon oil, to a level comparable to that of a newly prepared fresh titania catalyst before use. The method of reactivating a used titania catalyst for hydrogenation treatment, the used titania catalyst for hydrogenation treatment being obtained by supporting a catalyst component on a titania support and exhibiting reduced catalytic activity after having been used for hydrogenation treatment of a hydrocarbon oil, includes: a coke removal step of removing a carbonaceous component on a surface of the used catalyst by heating the catalyst in an oxygen-containing gas atmosphere; an impregnation step of impregnating the carbonaceous component-removed catalyst obtained by the coke removal step with a saccharide-containing solution; and a drying step of drying the saccharide-impregnated catalyst obtained by the impregnation step, to obtain a catalyst in which a saccharide is supported. 1. A method of reactivating a used titania catalyst for hydrogenation treatment , the used titania catalyst for hydrogenation treatment being obtained by supporting a catalyst component on a titania support and exhibiting reduced catalytic activity after having been used for hydrogenation treatment of a hydrocarbon oil ,the method comprising:a coke removal step of removing a carbonaceous component on a surface of the used catalyst by heating the catalyst in an oxygen-containing gas atmosphere;an impregnation step of impregnating the carbonaceous component-removed catalyst obtained by the coke removal step with a saccharide-containing solution; anda drying step of drying the saccharide-impregnated catalyst obtained by the impregnation ...

Furan-2,5-dicarboxylic acid purge process

Disclosed is an oxidation process to produce a crude carboxylic acid product carboxylic acid product. The process comprises oxidizing a feed stream comprising at least one oxidizable compound to generate a crude carboxylic acid slurry comprising furan-2,5-dicarboxylic acid (FDCA) and compositions thereof. Also disclosed is a process to produce a dry purified carboxylic acid product by utilizing various purification methods on the crude carboxylic acid.

PLANT AND PROCESS FOR TREATING A STREAM COMPRISING HYDROGEN SULFIDE

Installation and method for treating a flow comprising hydrogen sulfide The invention relates to an installation and a method for treating hydrogen sulphide. In particular, the invention relates to an installation and a method comprising at least one system for oxidizing hydrogen sulfide to sulfur (S) and water (HO) with a solid reagent and at least one oxidizing system with an agent for oxidizing the solid reagent present in the reduced state, wherein the system of oxidizing the hydrogen sulfide to sulfur and the system for oxidizing the solid reagent, are so arranged that the hydrogen sulfide is not brought into contact with the agent oxidizing the solid reagent. 1. A hydrogen sulfide treatment installation , wherein the installation comprises at least one system configured to oxidize hydrogen sulphide to sulfur (S) to water (HO) by a solid reagent implementing the reaction HS+sol-O→sol-R+HO+Swherein sol-O and sol-R respectively symbolize constituents of the solid reagent in oxidized and reduced forms , and at least one oxidizing system with an oxidizing agent of the solid reagent present in the reduced state , wherein the system oxidizing the hydrogen sulfide and the system oxidizing the solid reagent are so arranged that the hydrogen sulfide is not brought into contact with the agent oxidizing the solid reagent.2. The installation according to claim 1 , comprising a supply duct for a flow comprising hydrogen sulfide to a hydrogen sulfide oxidizing system in sulfur and water and a duct for discharge of a flow comprising sulfur.3. The installation according to claim 2 , comprising downstream of the system oxidizing the hydrogen sulfide in gaseous sulfur claim 2 , a sulfur separator of the flow initially comprising sulfur.4. The installation according to claim 1 , wherein the installation comprises one or more switch(es) configured to switch between the inlet of the hydrogen sulfide in the system oxidizing the hydrogen sulfide to sulfur and the inlet of the agent ...

METHOD FOR PRODUCING TETRAFLUOROPROPENE

The present invention concerns a method for preparing tetrafluoropropene utilising three reactors and comprising the steps of (a) implementing, in the first and second reactors, at least one step of reacting, in the gas phase, a compound B in the presence of hydrofluoric acid and a catalyst, in alternation with a step of regenerating the catalyst by bringing it into contact with a regeneration flow comprising an oxidising agent, (b) implementing, in the third reactor, a preliminary step of producing the compound B, in alternation with a step of regenerating the preliminary catalyst with a regeneration flow comprising an oxidising agent. The step of regenerating the preliminary catalyst in the third reactor is implemented in the absence of a step of reacting the compound B in the presence of hydrofluoric acid in said first and second reactors. The present invention also concerns a facility configured to implement the present method. 118-. (canceled)20. The process as claimed in claim 19 , further comprising:collecting a stream of products on conclusion of the preliminary stage of manufacture of the compound B;using said stream of products in order to carry out the stage of reaction of the compound B in the presence of hydrofluoric acid; andseparating the stream of products resulting from the stage of reaction of the compound B in the presence of hydrofluoric acid into a first stream comprising hydrochloric acid and tetrafluoropropene and a second stream comprising hydrofluoric acid and the compound B;optionally, collecting said second stream comprising hydrofluoric acid and the compound B, and the recycling said second stream in the stage of reaction of the compound B with hydrofluoric acid or of the preliminary stage of manufacture of the compound B.21. The process as claimed in claim 19 , wherein the stage of regeneration of the preliminary catalyst in the third reactor is carried out simultaneously with the stage of regeneration of the catalyst in the first ...

POLYMERIZATION SYSTEM HAVING A REGENERATION DEVICE FOR AN ADSORPTIVE AND/OR CATALYTIC CLEANING DEVICE, REGENERATION DEVICE, AND REGENERATION METHOD

A polymerisation system for obtaining at least one polymerisation product from at least one gaseous, hydrocarbon-rich feed stream, which system has at least one catalytic and/or adsorptive cleaning device for the at least partial extraction of at least one undesirable component in the at least one feed stream and a regeneration device for the regeneration of the cleaning device. The regeneration device is designed to at least intermittently condition and conduct a regeneration gas stream through the cleaning device by means of a partially closed gas circuit. There is further provided a corresponding regeneration method. 1. A polymerization plant for obtaining at least one polymerization product from at least one gaseous , hydrocarbon-rich feed stream , having at least one catalytic and/or adsorptive purifying unit for at least partial removal of at least one unwanted component in the at least one feed stream , and having a regenerating unit for regeneration of the purifying unit , characterized in that the regenerating unit is set up for at least temporary conditioning and guiding of a regeneration gas stream through the purifying unit by means of a partly closed gas circuit.2. The polymerization plant as claimed in claim 1 , wherein at least one heating unit claim 1 , at least one cooling unit and/or at least one compressor are arranged in the gas circuit.3. The polymerization plant as claimed in claim 1 , wherein the gas circuit has at least one feed unit and/or at least one withdrawal unit for a gas stream.4. The polymerization plant as claimed in claim 1 , wherein the purifying unit comprises a plurality of purifying vessels each filled with a purifying medium and the regenerating unit is set up for alternative or simultaneous guiding of the regeneration gas stream through at least two purifying vessels.5. The polymerization plant as claimed in claim 1 , wherein the regenerating unit is set up for operation in different operating phases in which the regeneration ...

CATALYTIC GAS PHASE FLUORINATION

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

METHOD AND PLANT FOR PRODUCING TETRAFLUOROPROPENE

A plant for the manufacture of tetrafluoropropene comprises three reactors for reaction in the gas phase comprising a catalyst bed. The first and second reactor are each configured in order to be fed in turn by a device for feeding with a reaction stream comprising a compound B and hydrofluoric acid; and a device for feeding with a regeneration stream configured in order to feed the reactor with a regeneration stream comprising an oxidizing agent. The third reactor is configured in order to be fed in turn by a device for feeding with a reaction stream comprising a compound A and hydrofluoric acid; said compound A being different from said compound B; and a device for feeding with a regeneration stream configured in order to feed the reactor with a regeneration stream comprising an oxidizing agent. 1. A plant for the manufacture of tetrafluoropropene comprising three reactors for reaction in the gas phase comprising a catalyst bed , a device for feeding with a reaction stream comprising a compound B and hydrofluoric acid; and', 'a device for feeding with a regeneration stream configured in order to feed the reactor with a regeneration stream comprising an oxidizing agent; and, 'the first reactor and the second reactor for reaction in the gas phase being each configured in order to be fed in turn by a device for feeding with a reaction stream comprising a compound A and hydrofluoric acid, and optionally an intermediate collecting device connected at the outlet of the first reactor or of the second reactor; said compound A being different from said compound B; and', 'a device for feeding with a regeneration stream configured in order to feed the reactor with a regeneration stream comprising an oxidizing agent., 'the third reactor for reaction in the gas phase being configured in order to be fed in turn by2. The plant as claimed in claim 1 , configured so that claim 1 , when the first reactor is fed by the device for feeding with reaction stream claim 1 , the second ...

Activation of Low Metal Content Catalyst

Methods are provided for activation of catalysts comprising low amounts of a hydrogenation metal, such as low amounts of a Group 8-10 noble metal. The amount of hydrogenation metal on the catalyst can correspond to 0.5 wt % or less (with respect to the weight of the catalyst), or 0.1 wt % or less, or 0.05 wt % or less. Prior to loading a catalyst into a reactor, the corresponding catalyst precursor can be first activated in a hydrogen-containing atmosphere containing 1.0 vppm of CO or less. The thus first-activated catalyst can be transferred to a reactor with optional exposure to oxygen during the transfer, where it can be further activated using a hydrogen-containing atmosphere containing 3.0 vppm of CO or higher, to yield a twice-activated catalyst with high performance. The catalyst can be advantageously a transalkylation catalyst or an isomerization catalyst useful for converting aromatic hydrocarbons. 1. A method for activating a catalyst , comprising:(I) providing a catalyst precursor comprising 0.5 wt % or less of a hydrogenation metal and a molecular sieve, based on the total weight of the catalyst precursor;{'sub': '2', '(II) reducing the catalyst precursor in a first vessel in the presence of a first atmosphere comprising Hand 1.0 vppm or less of CO, based on the total volume of the first atmosphere, to obtain a reduced catalyst; and'}(III) transferring the reduced catalyst to a second vessel.2. The method of claim 1 , wherein the method further comprises:{'sub': '2', '(IV) exposing at least a portion of the reduced catalyst to a second atmosphere comprising 1.0 vol % or more O, based on the total volume of second atmosphere, for an exposure time of 0.1 hours or more, to obtain an exposed reduced catalyst.'}3. The method of claim 2 , wherein step (IV) is at least partially performed during step (III).4. The method of any of claim 1 , further comprising:{'sub': '2', '(V) treating the reduced catalyst or the exposed reduced catalyst in the second vessel in ...

COMPOSITE CATALYST, METHOD FOR PRODUCING COMPOSITE CATALYST, METHOD FOR PRODUCING LOWER OLEFIN AND METHOD FOR REGENERATING COMPOSITE CATALYST

A lower olefin by using a zeolite catalyst, a composite catalyst capable of further extending the lifetime of catalytic activity, a method for producing the composite catalyst, a method for producing a lower olefin by using the composite catalyst, and a method for regenerating a composite catalyst in the method for producing a lower olefin are provided. The composite catalyst is a catalyst for producing a lower olefin from a hydrocarbon feedstock. This composite catalyst is constituted of a zeolite being a crystalline aluminosilicate containing gallium and iron or iron and further having a framework with 8- to 12-membered ring, and of silicon dioxide. By using the composite catalyst, a lower olefin can be continuously produced over a long period of time. 1. A composite catalyst for producing a lower olefin from a hydrocarbon feedstock , comprising:a zeolite being a crystalline aluminosilicate containing gallium and iron or iron and further having a framework with 8- to 12-membered ring; andsilicon dioxide.2. The composite catalyst according to claim 1 , whereinthe zeolite is a crystalline aluminosilicate containing iron and gallium, andan acid density as a composition ratio of the number of moles of silicon to a sum of the number of moles of iron, gallium, and aluminum is 75.0 to 200.0, a composition ratio of the number of moles of gallium to a sum of the number of moles of iron, gallium, and aluminum is 0.1 to 0.4, and a composition ratio of the number of moles of iron to a sum of the number of moles of iron, gallium, and aluminum is 0.2 to 0.6.3. The composite catalyst according to claim 1 , whereinthe zeolite is a crystalline aluminosilicate containing iron, andan acid density as a composition ratio of the number of moles of silicon to a sum of the number of moles of iron and aluminum is 75.0 to 200.0, and a composition ratio of the number of moles of iron to a sum of the number of moles of iron and aluminum is 0.4 to 0.7.4. The composite catalyst according to ...

METHODS AND APPARATUS FOR REGENERATION OF CATALYST BEDS IN REACTORS

The present invention relates to catalyst beds and, more particularly, regeneration of the catalyst by contacting the catalyst bed with nitrogen-rich gas, such as, air. The catalyst beds are typically positioned within a reactor vessel, such as, fixed-bed catalyst reactors. The catalyst bed serves as a solid support upon which chemical react. As a result of operation of the reactors, over a period of time, solid matter deposits on at least a portion of the catalyst bed causing reduced activity of the catalyst. Thus, the catalyst regeneration systems and methods of the invention provide the ability to provide continued effectiveness of the catalyst. 1. A method of regenerating a catalyst bed having catalyst with solid matter deposited thereon , comprising:heating a nitrogen-rich gas to an elevated temperature to produce a heated nitrogen-rich gas;passing the heated nitrogen-rich gas through or over the catalyst bed; andcontacting the catalyst with the heated nitrogen-rich gas.2. The method of claim 1 , wherein the nitrogen-rich gas is air.3. The method of claim 1 , wherein the catalyst bed is positioned within a fixed-bed catalyst reactor vessel.4. The method of claim 3 , wherein regenerating the catalyst is conducted without removing the catalyst bed from the reactor vessel.5. The method of claim 3 , wherein the catalyst bed is removed from the reactor vessel for regenerating the catalyst.6. The method of claim 1 , wherein the solid matter deposited on the catalyst is selected from the group consisting of carbon particles claim 1 , coke deposits claim 1 , carbon-containing particles claim 1 , and mixtures thereof.7. A method of regenerating catalyst claim 1 , in a catalyst bed claim 1 , having solid matter deposited thereon and positioned in a reactor claim 1 , comprising:introducing a heated nitrogen-rich gas at an inlet of the reactor;allowing the heated nitrogen-rich gas to flow through an interior of the reactor;contacting the catalyst in the catalyst bed of 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. 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 ...

Catalyst for purification of co2 from chlorinated hydrocarbons

A process for the purification of CO 2 from chlorinated hydrocarbons and non-chlorinated hydrocarbons, comprising: contacting a CO 2 stream with a chromium oxide catalyst, wherein the stream comprises the CO 2 , and impurities, wherein the impurities comprise the non-chlorinated hydrocarbons and the chlorinated hydrocarbons; forming a purified CO 2 stream by interacting the impurities with the chromium oxide catalyst to form additional CO 2 and chromium chloride; and regenerating the chromium oxide catalyst by contacting the chromium chloride with an oxygen containing gas stream.

Rhenium Promoted Catalyst

A group V metal/rhenium-modified molecular sieve catalyst can be used in hydrocarbon conversion reactions. Embodiments can provide a toluene conversion of at least 30 wt % with selectivity to benzene above 40 wt % and to xylenes above 40 wt % and non-aromatics selectivity of less than 2.0 wt %.

Process for the oxidative regeneration of a deactivated catalyst and an apparatus therefor

The present invention relates to a process for the oxidative regeneration of a deactivated catalyst comprising molecular sieve to provide a regenerated molecular sieve catalyst, wherein said deactivated catalyst is from one or both of an oxygenate to olefin process and a olefin cracking process, said regeneration process comprising at least the steps of providing a regeneration gas stream comprising oxidant; treating the regeneration gas stream with a liquid adsorbent stream comprising an ethylene glycol in a contaminant absorption zone to remove at least a part of one or more of any water, any alkali metal ion and any alkaline earth metal ion present in the regeneration gas stream to provide a treated regeneration gas stream comprising oxidant; regenerating a deactivated catalyst comprising molecular sieve with the treated regeneration gas stream to provide a regenerated catalyst comprising regenerated molecular sieve.

PROCESS FOR CONVERTING PARAFFIN TO OLEFIN AND CATALYST FOR USE THEREIN

The invention relates to a process for converting paraffin to olefin comprising the following steps: (a) providing a hydrocarbon feedstock containing at least one paraffin having 1 to 12 carbon atoms and at least one olefin having 2 to 12 carbon atoms; (b) providing a catalyst containing at least one Group VIA and/or Group VIIA transition metal on a solid support; (c) pretreating the catalyst by contacting the catalyst with at least one reducing gas and at least one oxidizing gas; and (d) contacting the hydrocarbon feedstock and the pretreated catalyst at a temperature in the range of 200° C. to 600° C., preferably 320° C. to 450° C. and to a catalyst for use therein.

REGENERATION METHOD FOR CATALYTIC CRACKING REACTION

A regeneration method for catalytic cracking reaction, the method is applied in a catalytic reaction process of petroleum hydrocarbon materials, and the method comprises: feeding the regenerated and semi-regenerated catalyst from a regenerator separately into different positions of a reactor for reaction. A part of the semi-regenerated catalyst is firstly processed in a purification cooler for removing carried nitrogen, oxygen, carbon dioxide and impurity gases before being fed into the reactor. Spent catalyst or the purified and cooled semi-regenerated catalyst is fed into a catalyst mixing section of the reactor for controlling the temperature of the catalyst being contact with the oil material to be gasified, thereby achieving a three stage cycle of the catalyst in the reactor and a three stage control for the reaction outlets of the oil material gasification zone and the cracking reaction zone and the catalyst taking part in the reaction.

Neutral Complex Cleaning Solution and Regeneration Method for Denitration Catalyst with Calcium Poisoning

The invention belongs to the field of nitrogen oxide control in environmental protection science and technology, and particularly relates to the field of regeneration and utilization of SCR denitration catalyst with calcium poisoning, that is a neutral complex cleaning liquid and a regeneration method for denitration catalyst with calcium poisoning. The present invention uses a neutral polyether surfactant as a regeneration and calcium removal reagent to achieve a poisoned catalyst regeneration method with high calcium removal rate, low loss rate of active components and excellent recovery of denitrification activity; wherein the content of the polyether surfactant is in the range of 0.1-1 wt %; by the regeneration method of the present invention, the loading of active components which is required in the conventional regeneration process can be omitted, while the corrosion of equipment and catalyst can be reduced, thus capable of regenerating the denitration catalyst with high efficiency. 1. A neutral complex cleaning solution for denitration catalyst with calcium poisoning , characterized in that: said solution comprises active ingredients of polyether surfactant , said polyether surfactant is selected from one or a mixture of JFC-E (C8-10 Fatty alcohol ethoxylates) , NP-10 (POLYETHYLENE GLYCOL TRIMETHYLNONYL ETHER) , EL-60 (cremophor EL 60) and AEO9 (polyethyleneglycol (9) mono-dodecyl ether).2. The neutral complex cleaning solution for denitration catalyst with calcium poisoning according to claim 1 , characterized in that: said neutral complex cleaning solution consists of 0.1-1 wt % of polyether surfactant and deionized water.3. A regeneration method of denitration catalyst with calcium poisoning using the neutral complex cleaning solution for denitration catalyst with calcium poisoning according to claim 1 , comprising the steps of:Step 1: Removing impurities remaining on a surface and inside pores of a poisoned denitration catalyst and drying under room ...

METHOD FOR PREPARING A LIGHT OLEFIN WITH AN OXYGEN-CONTAINING COMPOUND

A method for improving the light olefin yield in the process of preparation of a light olefin using an oxygen-containing compound, more specifically, in which, a multi-stage dense phase fluidized bed comprising k secondary pre-carbon deposition zones (k≧1) and n secondary reaction zones (n≧1) is used as a reactor, and a multi-stage dense phase fluidized bed regenerator comprising in secondary regeneration zones (m≧2) is used as a main equipment, and by re-refining hydrocarbons with four or more carbons obtained in the separation section, or adding naphtha, gasoline, condensate oil, light diesel oil, hydrogenation tail oil or kerosene in the reaction zone, the method primarily solves the problems in the prior art of the uniformity of carbon deposition amount and the carbon content of the catalyst being difficult to control, and the light olefin yield being low. 1. A method for preparing a light olefin using an oxygen-containing compound , comprising the following steps:{'sup': st', 'th', 'st', 'th, 'b': '1', 'step a) in which a hydrocarbon with four or more carbons is introduced from k feeding branch lines of pre-carbon deposition zone in parallel into k secondary pre-carbon deposition zones in a dense phase fluidized bed reactor, and is brought into contact with a completely regenerated and/or fresh catalyst, so as to be converted into a light olefin product-containing stream, while forming a pre-carbon deposited catalyst; wherein the catalyst is passed sequentially through 1to ksecondary pre-carbon deposition zones, with carbon content thereof increasing gradually; wherein the dense phase fluidized bed reactor is divided by a material flow controller into a pre-carbon deposition zone and a reaction zone; and wherein the pre-carbon deposition zone of the dense phase fluidized bed reactor is divided by a material flow controller into k secondary pre-carbon deposition zones, with to ksecondary pre-carbon deposition zones being connected in sequence;'}{'sup': th', 'st ...

CALCINATION PROCESS TO PRODUCE ENHANCED ODH CATALYST

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

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 ...

FURAN-2,5-DICARBOXYLIC ACID PURGE PROCESS

Disclosed is an oxidation process to produce a crude carboxylic acid product carboxylic acid product. The process comprises oxidizing a feed stream comprising at least one oxidizable compound to generate a crude carboxylic acid slurry comprising furan-2,5-dicarboxylic acid (FDCA) and compositions thereof. Also disclosed is a process to produce a dry purified carboxylic acid product by utilizing various purification methods on the crude carboxylic acid. 1. A process to produce an impurity rich waste stream in a carboxylic acid process , said process comprising: (i) 2,5-diformylfuran in an amount ranging from about 150 ppm to about 2.0 wt %,', '(ii) levulinic acid in an amount ranging from about 150 ppm to about 2.0 wt %,', '(iii) succinic acid in an amount ranging from about 150 ppm to about 2.0 wt %, and', '(iv) acetoxy acetic acid in an amount ranging from about 150 ppm to about 2.0 wt %., 'contacting a mother liquor in a solvent recovery zone to produce said impurity rich waste stream; wherein said mother liquor stream comprises at least one of the following2. A process according to wherein said process further comprises routing a portion of said impurity rich waste stream to a solid-liquid separation zone to form a purge mother liquor stream.3. A process according to wherein said process further comprises routing a portion of said purge mother liquor stream to a mix zone to form an extraction feed stream.4. A process according to wherein said process further comprises routing said extraction feed stream to an extraction zone to form a purge stream claim 1 , a raffinate stream claim 1 , and an extract stream.5. A process according to wherein said solvent recovery zone comprises at least one evaporator.6. A process according to wherein impurity rich waste stream is a slurry with weight % solids greater than 10%.7. A process according to wherein impurity rich waste stream is a slurry with weight % solids greater than 30%.8. A process according to wherein impurity ...

Aromatization Catalysts With High Surface Area and Pore Volume

Regenerable aromatization catalysts having high surface area and pore volume, as well as methods for producing these catalysts, are disclosed. 113-. (canceled)14. A method of producing a catalyst , the method comprising:(a) contacting a zeolitic base with an alkaline earth metal-containing compound to form an alkaline earth metal exchanged zeolitic support;(b) calcining the alkaline earth metal exchanged zeolitic support at a peak calcining temperature of less than about 550° C. (1022° F.);(c) impregnating the calcined alkaline earth metal exchanged zeolitic support with a Group VIII transition metal-containing compound; and{'sup': '2', '(d) calcining the impregnated alkaline earth metal exchanged zeolitic support to produce a catalyst having a surface area of at least about 165 m/g.'}15. The method of claim 14 , wherein:the zeolitic base comprises a L-zeolite;the alkaline earth metal-containing compound comprises barium; andthe Group VIII transition metal-containing compound comprises platinum.16. The method of claim 15 , wherein step (a) is the only step in the method which utilizes a barium-containing compound.17. The method of claim 16 , wherein the peak calcining temperature in step (b) is in a range of from about 315° C. (600° F.) to about 538° C. (1000° F.).18. The method of claim 17 , wherein:the peak calcining temperature in step (b) is in a range of from about 399° C. (750° F.) to about 493° C. (920° F.); orthe method does not include a contacting step comprising a fluorine-containing compound; orthe method does not include a contacting step comprising a chlorine-containing compound other than the platinum-containing compound; orany combination thereof.19. A reforming process comprising:contacting a hydrocarbon feed with a supported aromatization catalyst under reforming conditions in a reactor system to produce an aromatic product; wherein the supported aromatization catalyst comprises:an alkaline earth metal exchanged zeolitic support; and(ii) a Group ...

PREPARATION OF BUTADIENE BY OXIDATIVE DEHYDROGENATION OF N-BUTENE AFTER PRECEDING ISOMERIZATION

The invention relates to a process for preparing 1,3-butadiene by heterogeneously catalysed oxidative dehydrogenation of n-butene, in which a butene mixture comprising at least 2-butene is provided. The problem that it addresses is that of specifying a process for economically viable preparation of 1,3-butadiene on the industrial scale, which is provided with a butene mixture as raw material, wherein the 1-butene content is comparatively low compared to the 2-butene content thereof, and in which the ratio of 1-butene to 2-butene is subject to variation. This problem is solved by a two-stage process in which, in a first stage, the butene mixture provided is subjected to a heterogeneously catalysed isomerization to obtain an at least partly isomerized butene mixture, and in which the at least partly isomerized butene mixture obtained in the first stage is then subjected, in a second stage, to oxidative dehydrogenation. The two-stage process leads to higher butadiene yields compared to the one-stage process. 1. Process for preparing 1 ,3-butadiene by heterogeneously catalysed oxidative dehydrogenation of n-butene , in which a butene mixture comprising at least 2-butene is provided ,characterized in thata) the butene mixture provided is subjected to a heterogeneously catalysed isomerization to obtain an at least partly isomerized butene mixture,b) and in that the at least partly isomerized butene mixture is then subjected to oxidative dehydrogenation.2. Process according to claim 1 ,characterized in thatthe isomerization is effected in such a way that 2-butene present in the butene mixture provided is isomerized to 1-butene, such that the 1-butene content in the at least partly isomerized butene mixture has increased compared to the butene mixture provided.3. Process according to claim 1 ,characterized in thatthe isomerization is effected in such a way that 1-butene present in the butene mixture provided is isomerized to 2-butene, such that the 1-butene content in 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.

OXYGEN TRANSFER AGENTS FOR THE OXIDATIVE DEHYDROGENATION OF HYDROCARBONS AND SYSTEMS AND PROCESSES USING THE SAME

A oxygen transfer agent useful for the oxidative dehydrogenation of saturated hydrocarbons includes at least one mixed oxide derived from manganese or compounds thereof, as well as a promoter, such as tungsten and/or phosphorus. The oxygen transfer agent may also include an alkali metal or compounds thereof, boron or compounds thereof, an oxide of an alkaline earth metal, and an oxide containing one or more of one or more of manganese, lithium, boron, and magnesium. A reactor is at least partially filled with the oxygen transfer agent in the form of a fixed or circulating bed and provides an unsaturated hydrocarbon product, such as ethylene and/or propylene. The oxygen transfer agent may be regenerated using oxygen. 1. An oxygen transfer agent for the oxidative dehydrogenation of unsaturated hydrocarbons , said oxygen transfer agent comprising: {'br': None, 'sub': 6', '8, 'RR′O'}, 'a mixed oxide having a cubic crystal lattice structure and a chemical formula ofwherein R is a first element, R′ is a second element that is different than the first element, and O is oxygen, anda promoter selected from the group consisting of Sm, Ga, Ti, W, Mo, V, Nb, Cr, K, Cs, Rb, P, and As.2. The oxygen transfer agent of claim 1 , wherein the oxide is selected from the group consisting of MgMnO claim 1 , CuPbOand NiMnO claim 1 , with MgMnO.3. The oxygen transfer agent of claim 1 , wherein the oxide is MgMnO.4. The oxygen transfer agent of further comprising an alkali metal or compounds thereof.5. The oxygen transfer agent of further comprising boron or compounds thereof.6. The oxygen transfer agent of further comprising an oxide of an alkaline earth metal.7. The oxygen transfer agent further comprising an oxide of manganese claim 1 , wherein the manganese has a valence state selected from 4+ claim 1 , 3+ claim 1 , 8/3+ claim 1 , and 2+.8. The oxygen transfer agent of further comprising at least one of NaBMgMnO claim 1 , NaBMnMgO claim 1 , NaMnO claim 1 , LiMnO claim 1 , MgMnBO claim 1 ...

FISCHER-TROPSCH SYNTHESIS

A method () of synthesising Fischer-Tropsch products () includes feeding a synthesis gas () to a moving-bed Fischer-Tropsch synthesis reactor () containing a Fischer-Tropsch catalyst in a moving catalyst bed and catalytically converting at least a portion of the synthesis gas () in the moving catalyst bed to Fischer-Tropsch products (). The Fischer-Tropsch products () are removed from the moving-bed Fischer-Tropsch synthesis reactor (). The method () further includes, while the moving-bed Fisher-Tropsch synthesis reactor () is on-line, withdrawing a portion () of the Fischer-Tropsch catalyst from the moving-bed Fischer-Tropsch synthesis reactor (), adding a reactivated Fischer-Tropsch catalyst () to the moving-bed Fischer-Tropsch synthesis reactor (), and adding a fresh Fischer-Tropsch catalyst (), in addition to the reactivated catalyst (), to the moving-bed Fischer-Tropsch synthesis reactor (). 1. A method of synthesising Fischer-Tropsch products , the method includingfeeding a synthesis gas to a moving-bed Fischer-Tropsch synthesis reactor containing a Fischer-Tropsch catalyst in a moving catalyst bed, catalytically converting at least a portion of the synthesis gas in the moving catalyst bed to Fischer-Tropsch products and withdrawing the Fischer-Tropsch products from the moving-bed Fischer-Tropsch synthesis reactor, withdrawing a portion of the Fischer-Tropsch catalyst from the moving-bed Fischer-Tropsch synthesis reactor;', 'adding a reactivated Fischer-Tropsch catalyst to the moving-bed Fischer-Tropsch synthesis reactor; and', 'adding a fresh Fischer-Tropsch catalyst, in addition to the reactivated catalyst, to the moving-bed Fischer-Tropsch synthesis reactor., 'the method further including, while the moving-bed Fisher-Tropsch synthesis reactor is on-line2. The method according to claim 1 , wherein at least a portion of the withdrawn Fischer-Tropsch catalyst is subjected to a reactivation treatment thereby to produce at least a portion of the reactivated ...

FURAN-2,5-DICARBOXYLIC ACID PURGE PROCESS

Disclosed is an oxidation process to produce a crude carboxylic acid product carboxylic acid product. The process comprises oxidizing a feed stream comprising at least one oxidizable compound to generate a crude carboxylic acid slurry comprising furan-2,5-dicarboxylic acid (FDCA) and compositions thereof. Also disclosed is a process to produce a dry purified carboxylic acid product by utilizing various purification methods on the crude carboxylic acid. 1. A process to produce a raffinate stream in a method for making a carboxylic acid , said process comprising:(i) oxidizing in an oxidation zone an oxidizable raw material stream comprising 5-(hydroxymethyl) furfural (5-HMF) in the presence of an oxidation solvent stream comprising a saturated organic acid having from 2-4 carbon atoms and a catalyst at a temperature of 100° C. to 220° C. to produce a crude carboxylic acid slurry; wherein said oxidation zone comprises at least one oxidation reactor; wherein said crude carboxylic acid slurry comprises furandicarboxylic acid; wherein said catalyst comprises cobalt, manganese and bromine; and wherein the yield of furandicarboxylic acid is greater than 90%;(ii) routing said crude carboxylic acid slurry to a solid liquid separation zone to produce a mother liquor stream comprising said catalyst and impurities; wherein said solid liquid separation zone comprises at least one pressure drum filter;(iii) routing at least a portion of said mother liquor stream to a mother liquor purge zone comprising a liquid-liquid extraction zone to produce an extract stream comprising impurities and an extract solvent, and a raffinate stream comprising catalyst solvent and oxidation catalyst; wherein at least a portion of said oxidation catalyst and/or catalyst solvent is optionally recycled to the oxidation zone; and wherein said oxidizable raw material stream comprises greater than 40% by weight of 5-HMF.2. The process according to wherein said catalyst comprises cobalt in a range from ...

HYDROGEN SULFIDE REMOVAL PROCESS

A process is presented to treat a process stream containing a hydrocarbon (oil and/or gas) and hydrogen sulfide with a liquid treatment solution containing a sulfur dye catalyst. The process stream can be within a pipeline, wellbore, subsea pipeline or a wellhead that contains hydrogen sulfide where the liquid treatment solution is injected at a predetermined point to define a scavenger zone such that the sulfur dye catalyst in the liquid treatment solution causes the sulfide from the hydrogen sulfide to react with the catalyst. The hydrocarbon component is separated substantially free of the hydrogen sulfide from a spent treatment solution containing spent sulfur dye catalyst which can then be fed to an oxidation vessel where it is contacted with an oxygen containing gas causing the sulfide to oxidize to thiosulfate and converting the spent sulfur dye catalyst to regenerated sulfur dye catalyst. The thiosulfate can be recovered, and the regenerated sulfur dye catalyst can be recycled as part of the liquid treatment solution. 1. A process to remove hydrogen sulfide from a hydrocarbon stream contained in a wellhead pipeline comprising:injecting a liquid treatment solution comprising a sulfur dye catalyst directly into a pipeline that is in fluid communication with a well bore, where the pipeline contains a hydrocarbon and hydrogen sulfide and the injection of the liquid treatment solution forms an admixture such that the hydrogen sulfide is absorbed into the liquid treatment solution and reacts to form a spent sulfur dye catalyst that is contained within the admixture;directing the admixture into a separator where treated hydrocarbon and dissolved gas is separated from a spent treatment solution comprising the spent sulfur dye catalyst and water;introducing the spent treatment solution into an oxidation vessel containing an oxygen containing gas;oxidizing sulfide that is bound to the sulfur dye catalyst in the oxidation vessel to form a regenerated sulfur dye ...

PROCESS AND APPARATUS FOR FLUIDIZING A REGENERATOR

Disclosed is a process and apparatus for recycling flue gas from a regenerator back to the regenerator to provide fluidization gas needs. Catalyst may be separated from the flue gas before recycle and the flue gas may be compressed before recycle to the regenerator. The process and apparatus reduces the size capacity of downstream product recovery equipment by reducing gases derived by oxidation in the process and reduces the potential for after burn in the regenerator. 1. A process for regenerating catalyst comprising:combusting coke from spent catalyst in a regenerator to provide regenerated catalyst and flue gas;discharging flue gas from said regenerator;separating catalyst from said flue gas discharged from said regenerator; andrecycling said flue gas to said regenerator.2. The process of further comprising compressing said flue gas discharged from said regenerator before recycling said flue gas to said regenerator.3. The process of further comprising removing catalyst from said flue gas discharged from said regenerator before recycling said flue gas to said regenerator.4. The process of further comprising compressing said flue gas after catalyst is separated from it to recycle said flue gas to said regenerator.5. The process of further removing catalyst from said flue gas discharged from said regenerator by cyclonic separation.6. The process of further comprising removing catalyst from said flue gas discharged from said regenerator by filtration.7. The process of wherein said regenerator comprises a regenerator vessel and recycling includes distributing said flue gas in said regenerator vessel.8. The process of further comprising combusting coke from said spent catalyst in a lower chamber of said regenerator vessel and disengaging catalyst from flue gas in an upper chamber of said regenerator and said distribution of said flue gas in said regenerator is distributed in said upper chamber.9. The process of wherein said regenerator includes a regenerator conduit ...

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 ...

HYDROCARBON CONVERSION PROCESS

The present invention relates to a hydrocarbon conversion process comprising contacting a hydrocarbon feed stream with a hydrocarbon conversion catalyst, wherein the hydrocarbon conversion catalyst comprises a first composition comprising a dehydrogenation drogenation active metal on a solid support; and a second composition comprising a transition metal and a doping agent on an inorganic support, wherein the doping agent is selected from zinc, gallium, indium, lanthanum, and mixtures thereof. 1. A hydrocarbon conversion process comprising contacting a hydrocarbon feed stream with a hydrocarbon conversion catalyst , wherein the hydrocarbon conversion catalyst comprises:a first composition comprising a dehydrogenation active metal on a solid support; anda second composition comprising a transition metal and a doping agent on an inorganic support, wherein the doping agent is selected from zinc, gallium, indium, lanthanum, and mixtures thereof.2. The hydrocarbon conversion process according to claim 1 , wherein the dehydrogenation active metal is selected from platinum claim 1 , palladium claim 1 , iridium claim 1 , chromium claim 1 , and mixtures thereof.3. The hydrocarbon conversion process according to claim 1 , wherein the solid support is selected from aluminium oxide claim 1 , silicon dioxide claim 1 , zirconium dioxide claim 1 , titanium dioxide claim 1 , magnesium oxide claim 1 , calcium oxide claim 1 , and mixtures thereof.4. The hydrocarbon conversion process according to claim 1 , wherein the transition metal is selected from molybdenum claim 1 , tungsten claim 1 , rhenium claim 1 , and mixtures thereof.5. The hydrocarbon conversion process according to claim 1 , wherein the inorganic support is selected from aluminium oxide claim 1 , silicon dioxide claim 1 , zirconium dioxide claim 1 , titanium dioxide claim 1 , zeolite claim 1 , and mixtures thereof.6. The hydrocarbon conversion process according to claim 1 , wherein the second composition further ...

Method of regeneration of a spent sulfuric acid catalyst from alkylation of olefins and alkanes via paired oxidation

A spent sulfuric acid catalyst from an alkylation unit is regenerated via a paired oxidation electrolysis, wherein active intermediates are generated via both anodic oxidation and cathodic reduction without adding an additional organic peroxide during the electrolysis. The organic impurities in the spent sulfuric acid catalyst are decomposed by the active intermediates, and removed therefrom via evaporation. 1. A method of regeneration of a spent sulfuric acid catalyst from alkylation of olefins and alkanes , said spent sulfuric acid catalyst containing organic impurities and water , said method comprising introducing said spent sulfuric acid catalyst into an electrolysis reactor containing an anode and a cathode , introducing air or O-containing gas into said spent sulfuric acid catalyst , and supplying electricity to said anode and said cathode , wherein the improvement comprises said cathode being O-diffusion cathode , and said air or O-containing gas being introduced into said spent sulfuric acid catalyst through the O-diffusion cathode , so that oxygen , and water and protons in the spent sulfuric acid catalyst undergo reduction reactions at the O-diffusion cathode , forming oxidants of hydrogen peroxide and hydroxyl free radicals , and thus at least a portion of the organic impurities are decomposed via reactions with oxygen and the so-formed oxidants.2. The method of wherein no organic peroxide is added to said spent sulfuric acid catalyst before or during said supply of electricity.3. The method of claim 1 , wherein said anode comprises a semiconductor photocatalyst claim 1 , and a photo energy or light radiation having a wavelength of 10 to 2000 nm is applied to said anode.4. The method of claim 3 , wherein said semiconductor photocatalyst comprises a metal oxide semiconductor.5. The method of claim 3 , wherein said semiconductor photocatalyst comprises Ti—TiO claim 3 , or TiO.6. The method of claim 1 , wherein said anode comprises platinum claim 1 , ...

Mixed Metal Oxide Catalyst useful for Paraffin Dehydrogenation

A catalyst, methods of making, and process of dehydrogenating paraffins utilizing the catalyst. The catalyst includes at least 20 mass % Zn, a catalyst support and a catalyst stabilizer. The catalyst is further characterizable by physical properties such as activity parameter measured under specified conditions. The catalyst may also be disposed on a porous support in an attrition-resistant form and used in a fluidized bed reactor. 1. A process for continuous dehydrogenation of paraffins having 2-8 carbon atoms , preferably propane or isobutane , comprising:{'sup': '−1', 'contacting said paraffins with a catalyst composition at a reaction temperature of 500-800° C., a space velocity of 0.1-25 hrand a pressure of 0.01-0.2 MPa for a reaction period in the range of 0.05 seconds to 10 minutes;'}regenerating the said catalyst with an oxygen-containing gas wherein said catalyst regeneration is performed at a reaction temperature of 500-800° C., a pressure of 0.01-0.2 MPa and a regeneration period ranging from 0.05 seconds to 10 minutes;wherein the catalyst composition comprises:a mixed metal oxide catalyst suitable for the dehydrogenation of paraffins having 2-8 carbon atoms, comprising a catalyst composition of the general formula (AC) (CS) (ST) whereina) AC (Active Catalyst) represents oxides of zinc (Zn) wherein the catalyst comprises at least 20 mass % Zn,b) CS (Catalyst Support) represents oxides of aluminum (Al), silicon (Si), and titanium (Ti) or mixtures thereof,c) ST (Support Stabilizer) represents oxides of metals selected from the group of cerium (Ce), dysprosium (Dy), erbium (Er), europium (Eu), gadolinium (Gd), lanthanum (La), neodymium (Nd), praseodymium (Pr), samarium (Sm), terbium (Tb), ytterbium (Yb), yttrium (Y), tungsten (W), zirconium (Zr), or mixtures thereof, and{'sup': '−1', 'characterizable by a Activity Parameter >90,000, Selectivity Parameter <0.5 and a stability parameter <0.005 using a test where the mixed metal oxide catalyst is loaded in a ...

COMBUSTION OF SPENT ADSORBENTS CONTAINING HPNA COMPOUNDS IN FCC CATALYST REGENERATOR

Supplemental heat required to raise the temperature of a regenerated catalyst to the minimum required to promote the catalyzed reaction in an FCC unit is provided by introducing adsorbent material containing HPNA compounds and HPNA precursors with the coked catalyst into the FCC catalyst regeneration unit for combustion. The HPNA compounds and HPNA precursors can be adsorbed on either a carbonaceous adsorbent, such as activated carbon, that is completely combustible and generates no ash, or on fresh or coked FCC catalyst that is recovered from an HPNA adsorption column that has treated the bottoms from a hydrocracking unit to remove the HPNA compounds and their precursors. 1. An integrated process for the combustion of an ash-free carbon-based spent adsorbent material containing HPNA compounds and HPNA precursors in an FCC catalyst regeneration unit to produce supplemental heat comprises:a. separating and drying the spent adsorbent material containing HPNA compounds and HPNA precursors recovered from an adsorbent column used to treat hydrocracking unit bottoms at a temperature in the range of from 20° C. to 80° C.;b. grinding the dried spent adsorbent material containing HPNA compounds and HPNA precursors to produce a free-flowing mass of ground adsorbent particles;c. introducing the free-flowing mass of ground adsorbent particles into the inlet of the FCC catalyst regeneration unit with coked FCC catalyst recovered downstream of the FCC reactor;d. combusting the ground adsorbent particles and coked catalyst mixture with a stream of oxygen-containing gas in the FCC catalyst regeneration unit to produce a sufficient quantity of hot gases to raise the temperature of the regenerated catalyst to the minimum temperature required in the FCC reactor;e. separating the gases from the hot regenerated catalyst; andf. transferring the hot regenerated catalyst from the FCC catalyst regeneration unit to a regenerated catalyst retention zone.2. The process of which includes mixing ...

METHODS AND SYSTEMS FOR REMOVING GAS CONTAMINANTS FROM FLOWING SOLIDS

A method for removing gas contaminants from flowing solids in a fluid catalytic cracking (FCC) process can include: catalytically cracking a hydrocarbon feedstock in the presence of a catalyst in a riser of a FCC unit to produce a hydrocarbon product; separating the hydrocarbon product from a spent catalyst to produce a hydrocarbon product stream; regenerating the spent catalyst in a regeneration gas comprising oxygen to produce a mixture comprising a regenerated catalyst and a gas contaminant at a first concentration; introducing a stripping gas and the mixture into a regenerated catalyst stripper to produce a regenerated catalyst stream comprising the regenerated catalyst, the stripping gas, and a gas contaminant at a second concentration that is reduced by 50% or greater as compared to the first concentration; and introducing the regenerated catalyst stream to the riser. 1. A method comprising:catalytically cracking a hydrocarbon feedstock in the presence of a catalyst in a riser of a fluid catalytic cracking (FCC) unit to produce a hydrocarbon product;separating the hydrocarbon product from a spent catalyst to produce a hydrocarbon product stream;regenerating the spent catalyst in a regeneration gas comprising oxygen to produce a mixture comprising a regenerated catalyst and a gas contaminant at a first concentration;introducing a stripping gas and the mixture into a regenerated catalyst stripper to produce a regenerated catalyst stream comprising the regenerated catalyst, the stripping gas, and a gas contaminant at a second concentration that is reduced by 50% or greater as compared to the first concentration; andintroducing the regenerated catalyst stream to the riser.2. The method of claim 1 , wherein the wherein the gas contaminant comprise N claim 1 , CO claim 1 , CO claim 1 , SO claim 1 , SO claim 1 , NO claim 1 , NO claim 1 , O claim 1 , CN claim 1 , or a low molecular weight cyanide.3. The method of claim 1 , wherein the hydrocarbon product stream ...

Furan-2, 5-dicarboxylic acid purge process

Disclosed is an oxidation process to produce a crude carboxylic acid product carboxylic acid product. The process comprises oxidizing a feed stream comprising at least one oxidizable compound to generate a crude carboxylic acid slurry comprising furan-2,5-dicarboxylic acid (FDCA) and compositions thereof. Also disclosed is a process to produce a dry purified carboxylic acid product by utilizing various purification methods on the crude carboxylic acid.

OXYGENATE CONVERSION FOR DISTILLATE FUEL PRODUCTION

Systems and methods are provided for upgrading of methane and/or small alkanes to distillate boiling range hydrocarbons. The upgrading is performed using a reaction system where various types of integration are provided from downstream reaction stages to upstream reaction stages. Such integration can include recycle of various reaction products as well as thermal integration. Having a reaction system that begins with reforming of hydrocarbons and finishes with production of distillate can enable unexpected synergies between downstream reaction stages and upstream reaction stages. 1. A method for producing distillate boiling range products , comprising:{'sub': '2', 'exposing a feed comprising reformable hydrocarbons and at least one recycle input to a reforming catalyst under reforming conditions to produce a reformed effluent comprising Hand CO;'}exposing at least a portion of the reformed product to a methanol synthesis catalyst under methanol synthesis conditions to produce a synthesis effluent comprising methanol;exposing a conversion feed comprising at least a portion of the methanol from the synthesis effluent to a conversion catalyst under conversion conditions to form a conversion effluent comprising olefins and to form coke on the conversion catalyst;passing at least a portion of the conversion effluent into a heat exchange stage to form a cooled conversion effluent and steam;exposing at least a portion of the cooled conversion effluent and a recycled naphtha boiling range feed to an oligomerization catalyst under oligomerization conditions to form an oligomerized effluent;separating a light ends product fraction, a naphtha boiling range product fraction, and a distillate boiling range product fraction from the oligomerized effluent, the recycled naphtha boiling range feed comprising at least a portion of the naphtha boiling range product fraction; and{'sub': 2', '2, 'combusting the coke on at least a portion of the conversion catalyst to regenerate the at ...

Componente catalisador, sistema de catalisador e alquilação, e processo de alquilação.

Catalyst composition and reactivation process useful for alkane dehydrogenations

A catalyst comprising a Group IIIA metal, a Group VIII noble metal, and an optional promoter metal, on a support selected from silica, alumina, silica-alumina compositions, rare earth modified alumina, and combinations thereof, doped with iron, a Group VIB metal, a Group VB metal, or a combination thereof, offers decreased reactivation time under air soak in comparison with otherwise identical catalysts. Reducing reactivation time may, in turn, reduce costs, both in inventory and capital.

Gel catalysts and process for preparing thereof

A gel composition substantially contained within the pores of a solid material for use as a catalyst or as a catalyst support in dehydrogenation and dehydrocyclization processes.

METHOD FOR REGENERATING CATALYSTS.

Process for decoking catalysts

Katalytisk omdannelse av oksygenater til olefiner

PROCEDURE FOR THE CONVERSION OF AN OLEPHINE OR A BLEND OF OLEFINS.

LA INVENCION SE REFIERE A UN PROCESO PARA LA CONVERSION DE UNA OLEFINA O DE UNA MEZCLA DE OLEFINAS EN UNA COLUMNA DE DESTILACION EN LA QUE TIENEN LUGAR TANTO UNA REACCION DE METATESIS COMO UNA REACCION DE ISOMERIZACION. LA INVENCION SE CARACTERIZA PORQUE EN LA SECCION SUPERIOR TIENE LUGAR UNA REACCION DE METATESIS Y PORQUE EN LA SECCION INFERIOR TIENE LUGAR UNA REACCION COMBINADA DE METATESIS Y DE ISOMERIZACION. LA REGENERACION DEL CATALIZADOR DESACTIVADO SE LLEVA A CABO MEDIANTE UN TRATAMIENTO CON UNA OLEFINA, SEGUIDO DE UN TRATAMIENTO CON UN GAS QUE CONTENGA OXIGENO Y POSTERIORMENTE CON UN GAS QUE CONTENGA NITROGENO. THE INVENTION REFERS TO A PROCESS FOR THE CONVERSION OF AN OLEPHINE OR OF A MIXTURE OF OLEFINS IN A DISTILLATION COLUMN IN WHICH A REACTION OF METATESIS AND A REACTION OF ISOMERIZATION TAKE PLACE. THE INVENTION IS CHARACTERIZED BECAUSE A METATESIS REACTION HAS A PLACE IN THE UPPER SECTION AND A COMBINED METATESIS AND ISOMERIZATION REACTION HAS A PLACE IN THE LOWER SECTION. REGENERATION OF THE DEACTIVATED CATALYST IS CARRIED OUT THROUGH A TREATMENT WITH AN OLEPHINE, FOLLOWED BY A TREATMENT WITH A GAS CONTAINING OXYGEN AND SUBSEQUENTLY WITH A GAS CONTAINING NITROGEN.

Process and apparatus for the regeneration of catalysts

Regeneration of reduced supported chromium oxide catalyst for alpha-olefin oligomerization

A process for producing liquid oligomers useful as lubricants from alpha-olefins feedstock, such as 1-decene. The olefins are oligomerized over a supported and reduced metal oxide catalyst from Group VIB of the Periodic Table to produce the oligomers. The chromium-on-silica oligomerization catalysts can be regenerated to allow repeated recycling of the catalyst with reduced losses in yield of the lubricant. The regeneration process is particularly useful to regenerate catalyst deactivated during the course of oligomerization at high temperatures to produce low viscosity HVI-PAO lubricant. The regeneration process is carried out by (i) purging the deactivated catalyst with inert gas to strip unreacted olefin and lubricant product; (ii) contacting the purged catalyst with a stream of oxidizing gas at an elevated temperature to oxidize the carbonaceous deposits; and (iii) cooling the catalyst and contacting it with a stream of reducing gas to reduce the metal component to a lower valence state.

Regenerated hydrocracking catalyst and method for producing a hydrocarbon oil

This regenerated hydrocracking catalyst is formed by regenerating a used hydrocracking catalyst which contains both a carrier containing zeolite and an amorphous composite metal oxide having solid acidity, and at least one type of active metal selected from the noble metals of group 8 to group 10 of the periodic table and supported on the aforementioned carrier; relative to the total mass of the catalyst, this regenerated hydrocracking catalyst contains 0.05-1 mass% of a carbonaceous material in terms of carbon atoms.

Heterogeneous catalyst regeneration

heterogeneous catalyst regeneration method

Method for regeneration of catalyst used for cyclizing aminonitrile-to-lactam hydrolysis and utilization of regenerated catalyst for production of lactams

FIELD: industrial organic synthesis catalysts. SUBSTANCE: regeneration is accomplished by treating exhausted catalyst or working cycle-end catalyst with oxidative atmosphere at 300 to 600 C. EFFECT: achieved activity of regenerated catalyst comparable with that of fresh catalyst. 15 cl, 2 ex о69%50сс ПЧ сэ (19) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ ВИ “” 2 205 690 ' (51) МПК? 13) С2 В 01 4 38/12, 38/14, 38/16, 38/20, С 070 201/08 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 2001104900/04, 15.07.1999 (24) Дата начала действия патента: 15.07.1999 (30) Приоритет: 22.07.1998 ЕК 9809528 (46) Дата публикации: 10.06.2003 (56) Ссылки: ОЕ 2126007 А2, 15.03.1979. ЕР 0388070 АЛ, 19.09.1990. ОЕ 2641429 АЛ, 16.03.1978. УР 47033087 АТ, 16.11.1972. \МО 96/229174 АЛ, 01.08.1996. (85) Дата перевода заявки РСТ на национальную фазу: 22.02.2001 (86) Заявка РСТ: ЕК 99/01729 (15.07.1999) (87) Публикация РСТ: М/О 00/04994 (03.02.2000) (98) Адрес для переписки: 129010, Москва, ул. Б. Спасская, 25, стр.3, ООО "Юридическая фирма Городисский и Партнеры", пат.пов. Н.Г. Лебедевой, рег.№ 0112 (71) Заявитель: _ РОДИА ФАИБЕР ЭНД РЕЗИН ИНТЕРМЕДИЭИТС (ЕК) (72) Изобретатель: БРЮНЕЛЛЬ Жан-Пьер (ЕК), НЕДЕЗ Кристоф (ЕК) (73) Патентообладатель: РОДИА ФАИБЕР ЭНД РЕЗИН ИНТЕРМЕДИЭЙТС (ЕВ) (74) Патентный поверенный: Лебедева Наталья Георгиевна (54) СПОСОБ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРА ЦИКЛИЗИРУЮЩЕГО ГИДРОЛИЗА АМИНОНИТРИЛА В ЛАКТАМ И ИСПОЛЬЗОВАНИЕ РЕГЕНЕРИРОВАННОГО КАТАЛИЗАТОРА ДЛЯ ПРОИЗВОДСТВА ЛАКТАМОВ (57) Изобретение относится к способу регенерации катализатора циклизирующего гидролиза аминонитрила с целью получения лактамов. Предложен способ генерации твердых катализаторов, используемых в способах производства лактамов циклизирующим гидролизом аминонитрилов. Процесс регенерации состоит в обработке отработавшего катализатора или катализатора в конце рабочего цикла при температуре от 300 до 600°С окислительной атмосферой. Предложен способ использования регенерированных ...

An improved process for the conversion of hydrocarbons

539.385. Catalysts; cracking hydrocarbons. STANDARD OIL CO. Oct. 4, 1939, No. 27219. Convention date. Dec. 31, 1938. [Classes 1 (i) and 32] A catalyst for cracking hydrocarbons consists of silica gel which has been treated with a thorium salt and dried, whereby a thin coating of thorium compound is applied to the internal pore surface of the gel. The deposition is effected in acid solution. Heavy hydrocarbon oils are converted into gasoline by subjecting them in vapour phase to the action of the catalyst at 700-1050‹F.

Process for reactivation of sulfur deactivated cobalt titanium catalysts, catalyst composition, use of the reactivated catalysts to carry out carbon monoxide hydrogenation reactions and the products of such reaction

Polymerization plant with regenerating device for adsorptive and / or catalytic purification device, regenerating device and regeneration method

Es wird eine Polymerisationsanlage (100) zur Gewinnung wenigstens eines Polymerisationsprodukts (1) aus wenigstens einem gasförmigen, kohlenwasserstoffreichen Einsatzstrom (1, 2) vorgeschlagen, die wenigsten eine katalytische und/oder adsorptive Reinigungseinrichtung (20) zur wenigstens teilweisen Entfernung wenigstens einer unerwünschten Komponente in dem wenigstens einen Einsatzstrom (1, 2) und eine Regeneriereinrichtung (10) zur Regeneration der Reinigungseinrichtung (20) umfasst. Die Regeneriereinrichtung (10) ist zum wenigstens zeitweisen Konditionieren und Führen eines Regeneriergasstroms (4) durch die Reinigungseinrichtung (20) mittels eines teilweise geschlossenen Gaskreislaufs (11) eingerichtet. Ein entsprechendes Regenerierverfahren ist ebenfalls Gegenstand der vorliegenden Erfindung. A polymerization plant (100) is proposed for obtaining at least one polymerization product (1) from at least one gaseous, hydrocarbon-rich feed stream (1, 2), the at least one catalytic and / or adsorptive cleaning device (20) for at least partially removing at least one undesired component the at least one feed stream (1, 2) and a regeneration device (10) for regeneration of the cleaning device (20). The regeneration device (10) is set up for the at least temporary conditioning and guiding of a regeneration gas flow (4) by the cleaning device (20) by means of a partially closed gas circulation (11). A corresponding regeneration method is likewise an object of the present invention.

METHOD FOR REGENERATING CATALYSTS.

Catalyst system for producing aromatic amines

The invention relates to a catalyst system suitable for hydrogenating aromatic nitro compounds (I) to form the corresponding aromatic amines (II), the catalyst system containing, as essential constituents: a component A selected from the group consisting of silicon carbide, corundum (alpha-Al 2 O 3 ) and slightly porous to non-porous zirconium oxide (ZrO 2 ); and a component B, containing B1 – a carrier substance selected from the group consisting of silicon dioxide, gamma-, delta- or theta-aluminum oxide Al 2 O 3 , titanium dioxide, zirconium dioxide and graphite, B2 – a metal or a plurality of metals selected from the group consisting of copper, nickel, palladium, platinum and cobalt, and optionally B3 – an additional metal selected from the group consisting of at least one metal selected from main group I, main group II, main group IV and sub-groups II, V, VI and VIII of the periodic table of the elements, the proportion of component A being in the range of 5 to 60 wt%, in relation to the total weight of the catalyst system, and the aromatic nitro compounds (I) being those of the general formula R-(NO 2 ) n , (I), and the aromatic amines (II) being those of the general formula R-(NH 2 ) n , (II), and the moieties R and indices n in formulas (I) and (II) having the following meaning: R is a substituted or unsubstituted aromatic C 6 -C 10 moiety and n is an integer from 1 to 5.

Heterogeneous Catalyst Regeneration

사용된 티타늄-포함 실리콘 옥사이드 촉매들은 최소한 400℃의 온도에서 산소-포함 기체 스트림의 존재하에서 사용된 촉매를 가열함으로써 재생되며, 그리고 난 뒤 티타늄 소스를 이용하여 포화되고 포화된 촉매를 하소하여 재활성화된 촉매를 형성한다. The titanium-comprising silicon oxide catalysts used are regenerated by heating the used catalyst in the presence of an oxygen-comprising gas stream at a temperature of at least 400 ° C, and then reactivating by calcining the saturated and saturated catalyst with a titanium source. Formed catalyst.

Method for regenerating deactivated catalyst for hydro-treating

FIELD: technological processes. SUBSTANCE: invention relates to a method for regenerating deactivated catalysts for hydrotreating diesel fuel. Described is a method for regenerating a deactivated hydrotreating catalyst, in which the deactivated catalyst is calcined at a temperature of not more than 650 °C. Next, the calcined catalyst is contacted with a reactivating solution containing 0.55–2.7 mol/l of citric acid in an aqueous solution containing 10–20 wt. % butyldiglycol and 10–20 wt. % diethylene glycol. Said catalyst discharged from the impregnator in a continuous stream is fed to the dryer. As a result a catalyst is obtained having a pore volume of 0.3–0.8 ml/g, specific surface area of 150–280 m 2 /g, the average pore diameter of 6–15 nm, containing, wt. %: Co(C 6 H 6 O 7 ) – 6.3–13.0; H 4 [Mo 4 (C 6 H 5 O 7 ) 2 O 11 ] – 8.6–11.2; H 3 [Co(OH) 6 Mo 6 O 18 ] – 6.2–7.7; H 6 [P 2 Mo 5 O 23 ] – 4.0–10.2; SO 4 2- – 0.7–2.6; PO 4 3- – 0.5–4.4; carrier – the rest. EFFECT: technical result consists in carrying out hydrotreatment of diesel fuel in the presence of a catalyst of the claimed chemical composition, to obtain diesel fuel containing not more than 10 ppm of sulfur at low starting temperatures of the process, which predicts a long catalyst lifetime. 8 cl, 2 tbl, 4 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 38/62 B01J 38/12 B01J 38/02 B01J 23/94 (11) (13) 2 674 157 C1 (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 38/62 (2018.08); B01J 38/12 (2018.08); B01J 38/02 (2018.08); B01J 23/94 (2018.08) (21)(22) Заявка: 2018128999, 07.08.2018 (24) Дата начала отсчета срока действия патента: Дата регистрации: Приоритет(ы): (22) Дата подачи заявки: 07.08.2018 (56) Список документов, цитированных в отчете о поиске: RU 2484896 C1, 20.06.2013. RU (45) Опубликовано: 05.12.2018 Бюл. № 34 2 6 7 4 1 5 7 R U 2351634 C2, 10.04.2009. WO 2017091400 А1, 01.06.2017. EP 3315195 А1, 02.05. ...

Process for regenerating a catalyst

用于选择性转化氧合物为芳族化合物的氧化铝粘结型催化剂

本发明提供了催化剂组合物，其包含沸石、氧化铝粘结剂、和选自Zn和/或Cd的12族过渡金属，所述沸石具有至少约10的Si/Al比和至少约340m 2 /g的微孔表面积，所述催化剂组合物包含基于所述催化剂组合物的总重量为约50重量％或更少的所述粘结剂，并具有至少约290m 2 /g的微孔表面积，约0.1至约1.3的12族过渡金属与铝的摩尔比，和至少一种以下特征：中孔隙性为约20m 2 /g至约120m 2 /g；当在约120℃的温度和约60托(8kPa)的2,2?二甲基丁烷压力下测量时，2,2?二甲基丁烷的扩散率大于约1x10 ?2 sec ?1 ；以及合并的微孔表面积和中孔隙性为至少约380m 2 /g。

将烷烃脱氢成烯烃的方法和用于该方法的基于铁的催化剂

本发明涉及将低级烷烃催化脱氢成相应的烯烃的方法，在该方法中使用负载在载体上的包括碳化铁的可再生催化剂。在该方法中加入了少量(低于100ppm)硫化合物，例如H 2 S。

再生加氢裂化催化剂及烃油的制造方法

本发明的再生加氢裂化催化剂，其将含有载体和负载于前述载体的选自元素周期表第8族～第10族的贵金属中的至少一种活性金属的已使用的加氢裂化催化剂再生而成，其中，所述载体包含沸石和具有固体酸性的非晶性复合金属氧化物，再生加氢裂化催化剂含有以催化剂的总质量为基准按碳原子换算计为0.05～1质量%的碳质物质。