СПОСОБ ПОЛУЧЕНИЯ АЛКЕНА

Изобретение относится к способу получения алкена из оксигената, включающему взаимодействие потока исходных реагентов, содержащего не менее одного реагента-оксигената и воду, с катализатором из гетерополикислоты на подложке при температуре, равной не менее 170°C. Способ инициируют с помощью процедуры запуска, включающей следующие стадии: (i) нагревание катализатора из гетерополикислоты на подложке до температуры, равной не менее 220°C; (ii) поддержание подвергнутого термической обработке катализатора из гетерополикислоты на подложке, полученного на стадии (i), при температуре, равной не менее 220°C, в течение времени, достаточного для удаления связанной воды из гетерополикислоты - компонента катализатора из гетерополикислоты на подложке; (iii) при поддержании катализатора из гетерополикислоты на подложке, полученного на стадии (ii), при температуре, равной не менее 220°C, взаимодействие катализатора из гетерополикислоты на подложке с потоком исходных реагентов, находящихся при температуре ...

МЕЗОПОРИСТЫЙ КАТАЛИЗАТОР НА ОСНОВЕ СМЕШАННОГО ОКСИДА, СОДЕРЖАЩИЙ КРЕМНИЙ

Изобретение относится к мезопористым катализаторам для получения бутадиена из этанола. Предложен мезопористый катализатор на основе смешанного оксида, содержащего кремний и по меньшей мере один металл M, выбранный из тантала, ниобия и их смесей, в котором массовое содержание металла M составляет от 0,1 и 20% от массы смешанного оксида, и кремний и металл М связаны ковалентной связью. Предложен также способ получения указанного катализатора и его применение для получения 1,3-бутадиена из этанола. Технический результат – снижение стоимости катализатора при сохранении его эффективности. 3 н. и 10 з.п. ф-лы, 4 табл., 9 пр., 1 ил.

ПРОИЗВОДСТВО ВОДОРОДА

Изобретение относится к производству водорода и этана из метана. Способ селективного получения водорода или этана включает выбор подходящей температуры, составляющей свыше 300˚С, при которой металлический катализатор и исходный газ, содержащий метан, дают продукт, имеющий регулируемое отношение водород/этан. При этом при температуре свыше 1300˚С образуется водород и твердый углеродный продукт, а при температуре свыше 300˚С - продукт, имеющий мольное отношение водород/этан по меньшей мере 5. Металлический катализатор включает наночастицы рутения. Причем мольное соотношение метана и катализатора составляет от 10:1 до 100000:1. Обеспечивается гибкий способ конверсии метана, позволяющий получать различные продукты без замены оборудования и катализатора, что позволяет повысить экономичность производства. 3 н. и 12 з.п. ф-лы, 1 ил., 2 табл.

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 ПЕРЕРАБОТКИ УГЛЕВОДОРОДНЫХ СОЕДИНЕНИЙ, СОДЕРЖАЩИХ НИТРИЛЬНЫЕ ИЛИ АМИННЫЕ ФУНКЦИОНАЛЬНЫЕ ГРУППЫ

Изобретение относится к способу переработки углеводородных соединений, содержащих по меньшей мере одну нитрильную (азотсодержащую) функциональную группу. Способ характеризуется тем, что он состоит в обработке упомянутых соединений на стадии гидродеазотирования путем реакции с водородом при абсолютном давлении водорода, лежащем в интервале от 0,1 до 10 МПа, при температуре, лежащей в интервале от 200°С до 500°С и в присутствии катализатора гидродеазотирования, причем нитрильные соединения выбраны из группы, содержащей метилглутаронитрил, этилсукцинонитрил, 2-пентеннитрил, 2-метил-2-бутеннитрил или их смеси, а также изомеры орто-TDA. Использование настоящего способа позволяет удалять азот из стоков, содержащих углеводороды. 8 з.п. ф-лы, 6 пр., 5 табл.

КАТАЛИЗАТОР, СОСТОЯЩИЙ ИЗ ПЕРЕХОДНОГО МЕТАЛЛА, НАНЕСЕННОГО НА ДИОКСИД КРЕМНИЯ ВЫСОКОЙ ЧИСТОТЫ, ДЛЯ МЕТАТЕЗИСА ОЛЕФИНА (ОЛЕФИНОВ)

Изобретение относится к катализатору на носителе для метатезиса и к способу метатезиса с использованием данного катализатора. Описан катализатор метатезиса, состоящий по существу из переходного металла или его оксида, или смесей таких металлов или их оксидов, нанесенного(-ых) на носитель из диоксида кремния высокой чистоты, содержащего менее 150 ч/млн магния, менее 900 ч/млн кальция, менее 900 ч/млн натрия, менее 200 ч/млн алюминия и менее 40 ч/млн железа. При взаимодействии чистого бутена-1 с указанным катализатором в условиях реакции метатезиса реакция обладает массовой селективностью по гексену-3, по меньшей мере 55 мас.%. Также описан способ осуществления метатезиса, включающий обеспечение контактирования исходного сырья с катализатором метатезиса в условиях реакции метатезиса, которые минимизируют или исключают реакции изомеризации по двойной связи. Технический результат - улучшение селективности катализаторов метатезиса по отдельным продуктам. 2 н. и 15 з.п. ф-лы, 2 табл.

СПОСОБ ГИДРИРОВАНИЯ БЕНЗОЛА, СМЕСЕЙ БЕНЗОЛА И ТОЛУОЛА, СМЕСЕЙ БЕНЗОЛА И КСИЛОЛА, ИЛИ ИЗОМЕРНОЙ СМЕСИ КСИЛОЛА, ИЛИ СМЕСЕЙ БЕНЗОЛА, ТОЛУОЛА И КСИЛОЛА, ИЛИ ИЗОМЕРНОЙ СМЕСИ КСИЛОЛА, СОДЕРЖАЩИХ СЕРНИСТЫЕ АРОМАТИЧЕСКИЕ СОЕДИНЕНИЯ, И СПОСОБ ИХ ДЕСУЛЬФИРОВАНИЯ

Изобретение относится к вариантам способа гидрирования бензола, смесей бензола и толуола, смесей бензола и ксилола или изомерной смеси ксилола или смесей бензола, толуола и ксилола или изомерной смеси ксилола, содержащих сернистые ароматические соединения, в одном из которых на первой стадии, при необходимости в присутствии водорода, содержание сернистых ароматических соединений снижают в присутствии десульфуризатора, содержащего медь и цинк в атомном отношении от 1:0,3 до 1:10 (стадия а), и на второй стадии бензол, смеси бензола и толуола, смеси бензола и ксилола или изомерной смеси ксилола или смеси бензола, толуола и ксилола или изомерной смеси ксилола гидрируют в присутствии нанесенного на носитель рутениевого катализатора, содержащего от 0,01 до 30 мас.% рутения, в пересчете на общую массу катализатора, в присутствии водорода (стадия b). Также изобретение относится к способу десульфуризации, использующему тот же самый десульфуризатор. Применение настоящего способа позволяет получать ...

СПОСОБ ОЛИГОМЕРИЗАЦИИ ПРОПИЛЕНА

Сущность изобретения: пропилен олигомеризуют в присутствии рентгенографически аморфного алюмосиликагельного катализатора с молярным соотношением диоксида кремния и оксида алюминия 30 : 1 - 500 : 1, площадь поверхности 500 - 1000 м/г, общим объемом пор между 0,3 и 0,6 мл/г, средним диаметром пор порядка 10 или меньше, и свободными или в основном свободными порами с диаметром более, чем 30, при температуре 100 - 250°С и давлении 10 - 70 атм. 3 з.п. ф-лы, 1 табл.

РЕГЕНЕРАЦИЯ КАТАЛИЗАТОРОВ ДЕГИДРИРОВАНИЯ АЛКАНОВ

... 1. Способ дегидрирования алканов, по которому ! - смесь, содержащую углеводород, в частности алканы, которая может содержать водяной пар и, по существу, не содержит кислорода, подают непрерывно через слой катализатора при обычных условиях дегидрирования, ! отличающийся тем, что ! - сразу вслед за многочасовой стадией дегидрирования идет стадия с перепуском бескислородного газа через реакторный слой для продувки и для удаления реакционного газа из реакторного слоя, и ! - вслед за этим идет стадия перепуска кислородсодержащего регенерационного газа для удаления образованных из-за реакции дегидрирования отложений на катализаторе, и ! - вслед за этим идет стадия перепуска бескислородного газа для продувки и для удаления регенерационного газа из реактора, причем ! - продолжительность времени перепуска кислородсодержащего газа при регенерации катализатора составляет 70% от полной длительности регенерации или меньше. ! 2. Способ по п.1, отличающийся тем, что продолжительность времени регенерации ...

НЕ ПОДВЕРЖЕННЫЙ СПЕКАНИЮ КАТАЛИЗАТОР ГИДРИРОВАНИЯ И ДЕГИДРИРОВАНИЯ И СПОСОБ ЕГО ПОЛУЧЕНИЯ

... 1. Катализатор гидрирования и дегидрирования, включающий, по меньшей мере, один наночастичный палладиевый кластер и проницаемую для газов и жидкостей содержащую оксид циркония оболочку. ! 2. Катализатор по п.1, отличающийся тем, что наночастичный палладиевый кластер обладает средним показателем распределения по размерам (d50) в интервале от 0,1 до 100 нм и внутренний диаметр содержащей оксид циркония оболочки составляет от 10 до 1000 нм. ! 3. Катализатор по п.1 или 2, отличающийся тем, что толщина содержащей оксид циркония оболочки составляет от 10 до 100 нм. ! 4. Способ гидрирования органических соединений посредством водорода в газовой фазе в присутствии катализатора, отличающийся тем, что применяют катализатор по одному из пп.1-3. ! 5. Применение катализатора по одному из пп.1-3 для гидрирования или переносного гидрирования нитросоединений или в реакциях дегидрирования. ! 6. Применение по п.5, причем катализатор применяют для гидрирования нитросоединений в жидкой или газовой фазе при ...

ПРОИЗВОДСТВО ВОДОРОДА

... 1. Способ селективного получения водорода или этана из метана, включающийвыбор подходящей температуры, при которой металлический катализатор и исходный газ, содержащий метан, дают продукт, имеющий регулируемое соотношение водорода и этана, преимущественно водород и твердый углеродный продукт или преимущественно этан и водород;осуществление контакта исходного газа с металлическим катализатором при выбранной температуре для получения продукта.2. Способ по п. 1, в котором выбранная температура представляет собой температуру, подходящую для получения продукта, у которого соотношение водорода и этана составляет по меньшей мере 3.3. Способ по п. 1, в котором выбранная температура представляет собой температуру, подходящую для получения продукта, у которого соотношение водорода и этана составляет по меньшей мере 5.4. Способ по п. 1, в котором выбранная температура представляет собой температуру, подходящую для получения газообразного продукта, у которого соотношение водорода и этана составляет ...

ИНТЕГРИРОВАННЫЙ ПРОЦЕСС ПОЛУЧЕНИЯ АЛКЕНИЛЗАМЕЩЕННОГО АРОМАТИЧЕСКОГО СОЕДИНЕНИЯ

... 1. Интегрированный процесс получения С2-5-алкенилзамещенного ароматического соединения и водорода из С2-5-алкана и C6-12-ароматического соединения, включающий: (a) взаимодействие C2-5-алкана и C2-5-алкилзамещенного ароматического соединения в реакторе дегидрирования в присутствии катализатора дегидрирования в условиях процесса, достаточных для получения выходного потока дегидрирования, включающего С2-5 -алкенилзамещенное ароматическое соединение, С2-5-алкилзамещенное ароматическое соединение, С2-5-алкан, С2-5-алкен и водород; (b) разделение выходного потока дегидрирования в условиях, достаточных для получения практически неароматического газового потока, включающего С2-5-алкан, С2-5-алкен и водород, и ароматического потока, включающего С2-5-алкенилзамещенное ароматическое соединение и С2-5-алкилзамещенное ароматическое соединение, причем общее извлечение ароматических соединений составляет более чем примерно 90 мас.%; (c) подачу практически неароматического газового потока, включающего ...

СПОСОБ ПОЛУЧЕНИЯ АЛКЕНОВ ИЗ ОКСИГЕНАТОВ С ИСПОЛЬЗОВАНИЕМ НАНЕСЕННЫХ НА НОСИТЕЛЬ ГЕТЕРОПОЛИКИСЛОТНЫХ КАТАЛИЗАТОРОВ

... 1. Способ получения алкена (алкенов) из оксигенатного исходного материала в реакторе в присутствии нанесенного на носитель гетерополикислотного катализатора, отличающийся тем, что удельный объем его пор удовлетворяет следующей формуле: ! ОП>0,6-0,3 [количество ГПК/площадь поверхности высушенного катализатора], ! где ОП обозначает удельный объем пор высушенного, нанесенного на носитель гетерополикислотного катализатора (мл/г катализатора); ! количество ГПК представляет собой количество гетерополикислоты, содержащейся в высушенном, нанесенном на носитель гетерополикислотном катализаторе (мкмоль/г); ! площадь поверхности высушенного катализатора является удельной площадью поверхности высушенного, нанесенного на носитель гетерополикислотного катализатора (м2/г). ! 2. Способ по п.1, в котором количество гетерополикислоты на площадь поверхности нанесенного на носитель гетерополикислотного катализатора превышает 0,1 мкмоль/м2. ! 3. Способ по п.1, в котором нанесенный на носитель гетерополикислотный ...

КАТАЛИЗАТОР И СПОСОБ АРОМАТИЗАЦИИ С-СГАЗОВ, ЛЕГКИХ УГЛЕВОДОРОДНЫХ ФРАКЦИЙ АЛИФАТИЧЕСКИХ СПИРТОВ, А ТАКЖЕ ИХ СМЕСЕЙ

Изобретение относится к технологии переработки углеводородного сырья, в частности к катализаторам и технологии ароматизации углеводородных газов С-С, легких низкооктановых углеводородных фракций и кислородсодержащих соединений, а также их смесей с получением концентрата ароматических углеводородов. Катализатор содержит механическую смесь двух цеолитов. Первый цеолит охарактеризован силикатным модулем SiO/AlO=20. Цеолит предварительно обработан водным раствором щелочи и модифицирован оксидами редкоземельных элементов в количестве от 0,5 до 2,0 мас.% от массы первого цеолита. Второй цеолит охарактеризован силикатным модулем SiO/AlO=82. Цеолит содержит остаточные количества оксида натрия 0,04 мас.% от массы второго цеолита и модифицирован оксидом магния в количестве от 0,5 до 5,0 мас.% от массы второго цеолита. Цеолиты использованы в массовом соотношении от 1,7/1 до 2,8/1. Связующее содержит, по меньшей мере, оксид кремния и использовано в количестве от 20 до 25 мас.% от массы катализатора ...

КАТАЛИТИЧЕСКИ НЕАКТИВНЫЙ ТЕПЛОВОЙ ГЕНЕРАТОР И УСОВЕРШЕНСТВОВАННЫЙ ПРОЦЕСС ДЕГИДРИРОВАНИЯ

... 1. Система катализаторного слоя для использования в адиабатических неокислительных процессах дегидрирования, содержащая катализатор дегидрирования, включающий в себя следующие отдельные компоненты, физически соединенные друг с другом: ! a) активный компонент, выбранный из оксида металла Группы 4, Группы 5, Группы 6 и их сочетаний, и подложку, выбранную из оксида алюминия, глиноземов, моногидрата оксида алюминия, тригидрата оксида алюминия, оксида алюминия-оксида кремния, переходных оксидов алюминия, альфа-оксида алюминия, оксида кремния, силикатов, алюминатов, кальцинированных гидроталькитов, цеолитов и их сочетаний; ! b) первый инертный материал, в качестве которого выбран любой из материалов, которые являются каталитически неактивными в условиях реакции, в которых можно осуществить дегидрирование олефинов, и которые обладают высокой плотностью и высокой теплоемкостью, и которые не способны выделять тепло в ходе какой-либо стадии процесса дегидрирования; и ! c) вторичный компонент, содержащий ...

КАТАЛИТИЧЕСКАЯ КОНВЕРСИЯ АЛКАНОВ В АЛКЕНЫ

... 1. Способ каталитической реакции от С2 до С5 алкана и серосодержащего соединения для получения соответствующего алкена и сероводорода, в котором реакционную смесь вводят в контакт с катализатором при температуре от 300 до 650°С, в котором катализатор имеет площадь поверхности более 100 м2/г. 2. Способ по п.1, проводимый при температуре от 450 до 580°С. 3. Способ по п.1 или 2, в котором катализатор имеет площадь поверхности от 100 до 600 м2/г. 4. Способ по каждому из предшествующих пунктов, в котором алкан и серосодержащее соединение присутствуют в молярном отношении от 0,1 до 10 моль серы на 1 моль алкана. 5. Способ по п.4, в котором алкан и серосодержащее соединение присутствуют в молярном отношении от 0, 25 до 0,5 моль серы на 1 моль алкана. 6. Способ по каждому из предшествующих пунктов, в котором алкан представляет собой пропан. 7. Способ по каждому из предшествующих пунктов, в котором серосодержащее соединение представляет собой элементарную серу. 8. Способ по каждому из предшествующих ...

КАТАЛИЗАТОРЫ НА ОСНОВЕ КОБАЛЬТА

... 1. Способ получения предшественника катализатора на основе кобальта, включающий пропитку пористых частиц носителя для катализатора солью кобальта, частичную сушку пропитанного носителя и прокаливание частично высушенного пропитанного носителя с получением прокаленного продукта, содержащего исходную окись кобальта; частичное восстановление прокаленного продукта с тем, чтобы исходная окись кобальта частично восстановилась до СоО, с получением частично восстановленного продукта, и пропитку частично восстановленного продукта солью кобальта, частичную сушку пропитанного продукта и прокаливание частично высушенного пропитанного продукта с получением предшественника катализатора на основе кобальта. 2. Способ получения катализатора Фишера-Тропша на основе кобальта, включающий пропитку пористых частиц носителя для катализатора солью кобальта, частичную сушку пропитанного носителя и прокаливание частично высушенного пропитанного носителя с получением прокаленного продукта, содержащего исходную окись ...

Способ получения парафиновых и олефиновых углеводородов

VERFAHREN ZUR HERSTELLUNG VON OLEFINISCH UNGESAETTIGTEN ALIPHATISCHEN ODER CYCLOALIPHATISCHEN KOHLENWASSERSTOFFEN

VERFAHREN ZUR HERSTELLUNG VON AETHAN DURCH SELEKTIVE HYDROGENOLYSE VON ALKANEN

1,2-Di(4-isobutylphenyl)äthylen, dessen Herstellung und Verwendung als Zwischenprodukt.

FISCHER-TROPSCH CONVERSION OF SYNTHESIS GAS TO HYDROCARBONS

HETEROGENES ISOPARAFFIN/OLEFIN-ALKYLIERUNGSVERFAHREN.

UMWANDLUNG EINES NIEDRIGEN ALKANS.

PROCESS FOR THE PREPARATION OF ETHYLENE-ETHANE MIXTURES

Verfahren zur Umwandlung von Methanol zu flüssigen Kohlenwasserstoffen.

Verfahren zur Herstellung von Cyclohexan

Alkenkupplung.

Modifizierter Zeolith mit NES Struktur, und seine Verwendung für die Dismutation und/oder Transalkylierung von alkylaromatischen Kohlenwasserstoffen

VERFAHREN ZUR HERSTELLUNG VON AROMATISCHEN KOHLENWASSERSTOFFEN

ALUMINIUM-MODIFIZIERTE KIESELSAEURE, VERFAHREN ZU DEREN HERSTELLUNG UND DEREN VERWENDUNG

VERFAHREN ZUR OLIGOMERISIERUNG VON OLEFINEN ZU HOCHLINEAREN OLIGOMEREN UND KATALYSATOREN DAFÜR

VERFAHREN ZUR HERSTELLUNG VON ETHYLBENZOL

Ein auf einem metalloxid der Gruppe IVB basierende Katalysatorträger, seine Herstellung und seine Verwendungen

PROCESS FOR THE PREPARATION OF HYDROCARBONS

Verfahren zur Disproportionierung, Cyclisierung, Addition oder Polymerisation acyclischer, einfach ungesaettigter Olefinkohlenwasserstoffe

Verfahren zur katalytischen Disproportionierung acyclischer Olefine

New supported transition metal complex useful as catalyst in the transition metal catalyzed reaction, and in olefin metathesis reaction

Supported transition metal complex (T) based on a polystyrene matrix or silica gel matrix comprising a phenyl compound (I) or a phenyl-ketone compound (II), respectively, is new. Supported transition metal complex (T) based on a polystyrene matrix or silica gel matrix comprising a phenyl compound of formula (I) or a phenyl-ketone compound of formula (II), respectively, is new. X : a direct bond, O, S, -N(R 1>)-, -C(=O)O-, -O(O=)C-, -N(R 1>)(O=)C-, -C(=O)N(R 1>)-, -O-CHR 1>-O-, -OC(=O)N(R 1>)-, -N(R 1>)C(=O)O-, =C(=O) or =C(=S); R 1>, R 3>H or 1-4C alkyl; K 1>a transition metal complex; Z : a bond or a spacer; m, n, x, y : 1-5000; q : 2-5; and z : 3-20. An independent claim is included for a procedure for the transition metal catalyzed conversion of a reactant to a product in the presence of a supercritical carbon dioxide comprising using (T), as the catalyst. [Image] [Image].

Verfahren zur Herstellung von Olefinen durch Metathese an einem Carbid oder Oxicarbid eines Nebengruppenmetalls

Verfahren zur Herstellung von einer Verbindung mit einer nicht-aromatischen C-C-Doppel- oder -Dreifachbindung (Verbindung A) aus einer anderen Verbindung oder einer Mischung anderer Verbindungen mit einer nicht-aromatischen C-C-Doppel- oder -Dreifachbindung (Verbindung B), wobei man die Verbindung (B) bei einer Temperatur von 50 bis 500 DEG C mit einem heterogenen Katalysator, umfassend Carbide oder Oxycarbide eines Nebengruppenelements, in Kontakt bringt.

Katalytische Gewinnung von isomeren Hexenen

Methylbutenes - by pyrolysing vinyl isobutyrate over carrier catalysts contg copper oxide, giving high yields

Methylbutenes (I) are prepd. by pyrolysing vinyl isobutyrate (II) at 250-400 degrees C in presence of a carrier catalyst contg. 20-45 wt.% CuO. (I) is a raw material for prodn. of isoprene. (I) are the main prod. The temp. is pref. 330-380 degrees C. The catalyst carrier is esp. SiO2, pref. pptd. silicic acid, with particle size 3-50 m mu and surface area of about 240 m2/g; sodium silicate may also be used. Pyrolysis is in absence of moisture. (II) must be free from acids; (II) may be pre-treated with a base, or the pyrolysis catalyst may contain a solid base, e.g. 1-15 wt.% (pref. 2-10 wt.%) of alkali oxide or carbonate, esp. Na2CO3 or K2CO3. The catalyst may be prepd. by mixing 940 g. pptd. silicic acid with 1100 g. basic Cu carbonate (55.6 wt.% Cu) and 1600 g. water glass soln. (12.5 wt.% Na2SiO3), forming the mixt. into rods, drying at 120 degrees C for 16 hours and calcining at 345 degrees C for 16 hours. The gaseous (II) feed is pref. diluted with N2 to suppress resinification on ...

Improvements in and relating to the production of xylenes

Mixtures comprising p-xylene are produced by condensing acetone and acetylene in the presence of potassium hydroxide or alkoxide to yield 2, 5-dimethylhex-3-yne-2, 5-diol, dehydrating this to the yne-1, 5-diene, hydrogenating to give 2, 5-dimethylhexane, and contacting this in the vapour phase at elevated temperature with an aromatization catalyst. Acetone and acetylene may be introduced into potassium hydroxide in a suitable solvent at -10 to 20 DEG C., water then added, and the solvent layer dried, and distilled to yield the diol. Potassium alkoxides such as tert. butylate or iso-amylate may replace the hydroxide. The diol is converted to diene as described in Specification 702,332. Hydrogenation of the diene is preferably effected in liquid phase using, e.g. Gp. 8 metals such as Pt, Cu or Ni. Vapour phase hydrogenation may be effected, e.g. with Ni at 100-450 DEG C. Aromatization is effected catalytically as described in Specifications 698,954 and 702,360. In an example, the p condensation ...

HYDROCARBON CONVERSION CATALYST AND THE USES THEREOF

... 1474284 Catalytic hydroforming of hydrocarbon feedstocks EXXON RESEARCH & ENG CO 28 June 1974 [19 July 1973] 28783/74 Heading O [Also in Division B1] Hydrocarbon feeds are converted in the presence of a catalyst comprising at least 0À1% wt. of platinum, at least 0À1% wt. of iridium and at least 0À05% wt. of rhodium on a refractory oxide support wherein the noble metals are present as polymetallic clusters with a total metal carbon monoxide chemisorption surface area of at least 200 m2/g. The conversion process may be reforming using a halogen-containing catalyst containing less than two atoms of sulphur per atom of noble metals and being substantially free of alkali or alkaline earth metal constituents. Naphtha hydroforming of a substantially sulphur-free feed containing 10-80 vol. per cent paraffins, 10-80 vol. per cent naphthenes and 2-20% aromatics and boiling at 80-450‹ F. is described using vapour phase reaction at 650-1000‹ F., 1-50 atmos. pressure, a space velocity of 0À5 ...

Preparation of hydrogenation catalysts

... 1,146,876. Hydrogenation of hydrocarbons. SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ N.V. 24 Oct., 1967 [26 Oct., 1966], No. 47978/66. Heading C5E. [Also in Division B1] Hydrocarbons are hydrogenated using a catalyst prepared by mixing a Ni and/or Co salt solution with a silica sol, adding a base, separating, washing and drying the coprecipitate and heating it in a stream of H 2 or H 2 -containing gas at 150-600‹ C. Aromatics, e.g. benzene, may be hydrogenated to naphthenic compounds. The catalyst may be sulphided and is then particularly suitable for hydrogenating a diolefin to a mono-olefin, e.g. for improving the gum stability of a steam-cracked gasoline.

PROCESS FOR THE PREPARATION OF AN OLEFINS-CONTAINING MIXTURE OF HYDROCARBONS

CATALYST FOR THE CONVERSION OF HYDROCARBONS AND ITS MANUFACTURE AND USE

... 1327738 Catalyst composition INSTITUT FRANCAIS DU PETROLE DES CARBURANTS ET LUBRIFIANTS 1 March 1972 [3 March 1971] 9590/72 Heading B1E [Also in Division C5] A catalyst composition comprises: (a) a carrier which is alumina, silica, alumina-silica or magnesia; (b) 0.005-1% wt. with respect to the carrier of each of platinum and iridium; and (c) 0.005-1% at with respect to the carrier of zinc or a zinc compound (calculated as zinc oxide). The Examples describe compositions of gamma alumina, platinum, iridium, a zinc compound, e.g. the sulphate and, optionally, fluorine or chlorine. In Example 1 the composition is calcined then reduced in a stream of hydrogen before use.

Improvements in or relating to the polymerization of olefins

Normally gaseous olefins are polymerized at elevated temperature and pressure in the presence of a finely-divided solid catalyst comprising phosphoric acid deposited on a non-carbonaceous carrier, together with a divided solid adsorbent diluent for the catalyst. Said diluent is preferably impregnated with phosphoric acid, the amount of acid in the diluent, expressed as a percentage by weight thereof based on diluent+acid being at least 20 per cent less than the amount of acid in the catalyst expressed as a percentage by weight based on carrier+acid. The adsorbent diluent may be silica gel, bauxite, activated alumina, carbon or activated carbon. Silica gel is preferably de-activated before use to reduce the surface area to from 50-300 sq. m. per g., e.g. by heating at 1800 DEG F. for 3/4 -2 hours. Carbon should have a density near that of the catalyst. It may be treated with phosphoric acid solution, dried, and heated at 400-500 DEG F. The amount of diluent is generally 5-50 per cent by ...

Process for the activation of a catalyst

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

Improvements in the manufacture and production of hydrocarbons and their derivatives from mixtures of hydrogen and oxides of carbon

Hydrocarbons with or without oxygenated derivatives are obtained by reacting carbon monoxide and hydrogen in presence of a catalyst obtained by reacting previously fused ferrosoferric oxide with a reducing gas at a temperature above 300 DEG C. The catalyst may also contain compounds of silicon, titanium, heavy metals, nickel, cobalt, and/or alkali metals. The reaction may be effected at a temperature of 275--425 DEG C., and a pressure above 50 atmospheres. The catalyst may be prepared by fusing iron powder with the activating additions in a current of oxygen and subsequently reducing with hydrogen or gaseous hydrocarbons.ALSO:A catalyst for the production of hydrocarbons from carbon monoxide and hydrogen is obtained by reducing previously fused ferrosoferric oxide. Activating additions such as compounds of silicon, titanium, heavy metals, nickel, cobalt, and/or alkali metals may be present. The catalyst may be prepared by fusing iron powder with the activating substances in a blast of oxygen ...

PROCESS FOR THE PREPARATION OF HYDROCARBONS

A process for the preparation of Fischer-Tropsch catalysts

SiO2-supported Cr-promoted Fe- catalysts are prepared by impregnation, calcination and reduction at 350-750 DEG C. Hydrocarbons are prepared from H2-poor syngas with the use of this catalyst.

Process for the hydrogenation of hydrocarbons with non-terminal olefinic double bonds

Hydrocarbons having olefinic double bonds of which at least one is not in the end position are hydrogenated with excess hydrogen using a nickel catalyst on kieselguhr at an elevated temperature and under elevated pressure. The nickel content of this catalyst is 50 to 70% by weight, based on the total weight of the catalyst. The kiesselguhr has a specific surface area of 100 to 180 m<2>/g and contains, in addition to 85 to 93% by weight of SiO2, a further 3 to 8% by weight of Al2O3, 0.1 to 0.2% by weight of TiO2, 1 to 1,6% by weight of Fe-oxides, 0.1 to 0.7% by weight of MgO, 0.3 to 1% by weight of CaO and 0.7 to 1.5% by weight of alkali metal oxides, all based on the total weight of the kieselguhr. The LHSV is set at 0.1 to 8 litre of substrate per litre of reaction volume per hour.

PROCESS FOR THE PREPARATION OF HYDROCARBONS

Amorphous silica-based catalyst and process for its production

The catalyst comprises a highly porous amorphous silica having a monolayer of an amphoteric metal (e.g. Al, Zn, Mg, Zr, Ti) chemically bonded onto up to 90% of the surface area of the silica matrix. The catalyst has a maximum pore diameter of 1.5nm and the metal is preferably aluminium. The catalyst is produced by treating the silica with a solution of a hydrolysable aluminium compound, removing the solvent and causing the silica surface to hydrolyse the compound, thus chemically bonding the aluminium onto the surface of the silica matrix. Optionally, the catalyst is mixed intimately with a Fischer- Tropsch catalyst to enable the direct conversion of synthesis gas to hydrocarbons. The catalyst will be of use in the conversion of synthesis gas or methanol to higher hydrocarbons.

A fuel additive for use in alcohol fuels

A method for inhibiting corrosion and elastomer swelling and degradation caused by alcohol and alcohol-containing fuels and for increasing lubricity of alcohol or alcohol-containing fuels, comprising adding to the fuel a fuel additive comprising one or more reaction products of a carboxylic acid or acid chloride selected from the group consisting of unsubstituted aromatic carboxylic acids, aliphatic carboxylic acids, nitro-substituted aromatic carboxylic acids and their corresponding acid chlorides, and an amine selected from the group consisting of aliphatic amines, cycloaliphatic amines, and aromatic amines. The invention also provides a fuel composition for internal combustion engines, comprising: (a) a major portion of fuel comprising from 1 to 100% by volume of an alcohol having 1 to 4 carbon atoms and from 99 to 0% by volume of a non-alcohol fuel selected from the group consisting of gasoline, individual hydrocarbon components of gasoline, and dimethoxymethane, and (b) a minor portion ...

TELEVISION DEFLECTION CIRCUIT WITH RASTER WIDTH STABILIZATION

Reverse biased P-N Junction cathode

The invention relates to a semiconductor, cathode and a camera tube and a display tube, respectively, having such a cathode, based on avalanche breakdown in a p-n junction extending parallel to the surface of the semiconductor body. The released electrons obtain extra energy by means of an accelerating electrode provided on the device. The resulting efficiency increase makes the manufacture of such cathodes in planar silicon technology practical. Since the depletion zone of the p-n junction upon avalanche breakdown does not extend to the surface, the released electrons show a sharp, narrow energy distribution. This makes such cathodes particularly suitable for camera tubes. In addition they find application, for example, in display tubes and flat displays.

Process for the selective hydrogenation of hydrocarbon mixtures

Hydrocarbon mixtures containing compounds having more than one olefinic bond and/or at least one acetylenic bond, but substantially free from acetylene, are selectively hydrogenated to mono-olefins in the presence of a catalyst comprising at least one metal of Group Ib, i.e. copper, silver and gold, supported on an inert carrier. The process may be applied to hydrocarbon mixtures boiling below 216 DEG C., suitably those obtained by cracking processes, and these include full boiling range gasolines, narrow fractions thereof, and substantially pure butadiene and isoprene. The Group Ib metal may constitute 1-15% by weight of the total catalyst; silver and/or copper supported on silica gel is preferred. A preferred catalyst is made by impregnating the support with copper and/or silver complexed with a water-soluble nitrogen base, particularly ammonia or ethylene diamine, and calcining. Hydrogenation may be effected at 35-345 DEG C., at 1-50 atmospheres, and in the vapour, liquid or mixed phase ...

Method for preparing ceramic catalysts

A ceramic catalyst of formula AA'MM'X prepared using sol-gel and ceramic methodologies comprises preparing a sol or slurry in an organic acid, alcohol or water of an alkaline earth metal component (A) preferably barium or strontium; a powdered or liquid transition metal component (M') selected from germanium, lead, silicon, tin, aluminium, gallium, antimony, bismuth or niobium; a powdered metal component (M) wherein M is selected from titanium or zirconium; and X is oxygen/s. The formula may optionally comprise A' selected from samarium or indium; The components are refluxed or mixed together, and the powder is dried and heated with a temperature program to calcination temperatures. The catalyst is for converting methane to higher hydrocarbons by oxidative condensation (or coupling) of methane (OCM). The OCM catalyst may be mixed with a second catalyst of formula NBC/S, for CO2-reforming of methane or dehydrogenation of ethane to ethylene, wherein N is a metal selected from Group IA or ...

Process for the preparation of a Fischer-Tropsch catalyst a catalyst so prepared and use of this catalyst in the preparation of hydrocarbons

A Fischer-Tropsch catalyst is prepared by impregnating a silica carrier with a solution of a zirconium or titanium compound, calcining the composition thus obtained, thereafter impregnating the carrier with a cobalt compound-containing solution and calcining and reducing the composition thus obtained. Catalysts so prepared and containing 5-40 pbw of cobalt and 2-150 pbw of zirconium or titanium per 100 pbw of silica, are used in the preparation of hydrocarbons from a H2/CO mixture.

PREPARATION OF DIMETHYLNAPHTHALENES

Process for the catalytic polymerisation of normally gaseous olefins

... 532,381. Polymerization of olefines. UNIVERSAL OIL PRODUCTS CO. May 19, 1939, No. 14964. Convention date, June 15, 1938. Drawings to Specification. [Class 2 (iii)] Propylene and/or butylenes are polymerized to gasoline products by contact with a solid catalyst consisting of a pre-calcined mixture of a major proportion by weight of a phosphoric acid and a minor proportion by weight of a siliceous carrier such as kieselguhr, the temperature being maintained within the range of 204-288‹C. under a pressure exceeding 40 atmospheres but not exceeding 136 atmospheres. In the case of stabilizer refluxes composed principally of 3 and 4 carbon atom hydrocarbons, temperatures of 232-288‹C. and pressures of over 40 to about 54 atmospheres are employed. Fractions composed mainly of 3 carbon atom hydrocarbons require temperatures of . 232-260‹C. and pressures of more than 40 atmospheres even as high as 136 atmospheres, whilst in the case of butane-butene fractions temperatures of 204-260‹C. are used ...

HORIZONTAL DEFLECTION CIRCUIT

LIQUID HYDROCARBON SYNTHESIS

Separation of Olefines.

... 1,171,950. Separating olefins. IMPERIAL CHEMICAL INDUSTRIES Ltd. 1 Nov., 1968 [29 Nov., 1967], No. 54321/67. Heading C5E. Mixtures of branched and unbranched olefins are separated by selective dimerization of the branched olefin over a catalyst comprising a supported transition metal and/or a compound thereof. Preferred catalysts are oxides or sulphates of nickel or cobalt supported on alumina, silica or magnesia, particularly nickel oxide on silica/alumina. The process is suitably liquidphase, e.g. at 0-150‹ C. In examples the following mixtures are treated, the first-named being selectively dimerized: isobutene and propylene; isobutene and n-butene; and isobutene, nbutene and propylene. Selectivity is enhanced by the presence of minor amounts of polyunsaturated hydrocarbons, e.g. 0.2 wt. per cent of butadiene.

CATALYTIC CRACKING OF ISOBUTYRALDEHYDE

... 1,241,646. Butyraldehyde. RUHRCHEMIE A.G. 13 Feb., 1970 [3 April, 1969], No. 7099/70. Heading C2C. [Also in Division C5] In an oxo process for producing n-butyraldehyde as the desired product from propylene, carbon monoxide and hydrogen, the unwanted isobutyraldehyde also produced is catalytically cracked to yield propylene, carbon monoxide and hydrogen, which are recycled. The cracking is performed in the gaseous phase at 200- 400‹ C. under a pressure of 0À 1-20 -atmospheres, using a catalyst comprising rhodium and/or platinum.

DEHYDROCYCLODIMERISING C4 HYDROCARBONS

... 1496379 Dehydrocyclodimerizing C 4 hydrocarbons BRITISH PETROLEUM CO Ltd 13 Oct 1976 [20 Nov 1975] 47830/75 Heading C5E Aromatic hydrocarbons, particularly benzene, toluene and xylenes, are produced by dehydrocyclodimerizing a C 4 hydrocarbon feed in the presence of a catalyst comprising Ge, In or Sn, in metal or compound form, deposited on a support. The reaction may be carried out in the presence of H 2 or under an atmosphere of N 2 . The support may be Al 2 O 3 , SiO 2 , activated carbon or refractory Ga 2 O 3 . Surface hydroxyl groups on hydrated SiO 2 or hydrated Al 2 O 3 may be exchanged with ions of the catalytic metals and optionally also with ions of Ga, Al or Fe. Preferably the catalytic metals are present as oxides.

METHOD OF PRODUCTION OF ETHANE BY SELECTIVE HYDROGENOLYSIS OF ALKANES

... 1499622 Ethane by hydrogenolysis of alkanes SOC NATIONALE ELF AQUITAINE 23 June 1976 [30 June 1975 14 Nov 1975 16 Dec 1975] 26040/76 Heading C5E Ethane is produced by introducing into a reactor at a space velocity of 200-10,000 h-1 a mixture of H 2 and alkanes over a catalyst comprising Ir and/or Rh incorporated in a support of inert refractory oxide in which the SO 4 -- ion content is lower than 0À5 wt. per cent. The catalyst may further comprise another Group VIII metal selected from Os, Co, Pd, Fe, Ni, Ru and Pt. The total percentage of metal in the catalyst may be 0À1-10 wt. per cent. The hydrogenolysis may be carried out at 150-550‹ C. 1-80 bar and a mole ratio of H 2 : alkane of 2 to 20:1. The refractory support may be Al 2 O 3 , SiO 2 , SiO 2 -Al 2 O 3 , MgO, TiO 2 or ZnO. The ethane may be steam-cracked to give ethylene and the hydrogen produced recycled to the hydrogenolysis stage.

Production of conjugated diolefines

Conjugated diolefins are prepared by reacting a C2-C6 mono-olefin with formaldehyde or acetaldehyde at elevated temperature in the vapour phase in the presence of a catalyst containing 1-20% by weight of phosphoric acid (calculated as P2O5) on an inert support. The olefin is preferably a tertiary olefin, e.g. isobutene (to form isoprene) or 2-methylbutene-1 or -2 and is used in an amount of 1-20 mols per mol of aldehyde. Formaldehyde may be supplied as formalin, the water forming an inert diluent; suitably amounts of diluent up to 95% by volume of the reaction mixture may be employed, e.g. nitrogen, carbon dioxide or lower paraffins. The reaction is effected at 100-400 DEG C. at a space velocity of 0,1-50 mols of aldehyde per litre of catalyst per hour. The acid catalyst may be supported on silica gel or kieselguhr.

Isothermal methanation

Synthesis gas is formed into methane by successive contact steps with (a) a catalyst comprising a solid support having deposited thereon a metal selected from Fe, Co, Ni, Cu, W, Ru, Rh, Pd, Ir, Pt alloys of the said metals with each other and alloys containing an aggregate of at least 10% by weight of one or more of the said metals with other metals, and (b) an inert body or assembly of bodies having a substantial surface area with which the gases make contact subsequent to their contact with the said catalyst, the said inert body or assembly of bodies having sprayed on to it or them a liquid medium which removes heat from the gases such that the temperature of the gas emerging from the body or assembly of bodies is not higher than 600 DEG C. ...

Production of dialkylnaphthalenes

Dialkylnaphthalenes are obtained by adding, with stirring, an olefin to a mixture of naphthalene, monoalkyl-naphthalene and sulphuric acid in an amount of 1.2-5.9 parts by weight per part of naphthalene while maintaining a temperature of 0 DEG C.-15 DEG C. and recovering dialkylnaphthalenes; monoalkylnaphthalenes are preferably recycled. The process is particularly applicable to one employing a nonene (C6-C12, containing at east 40% by volume of C9) fraction of a propylene polymer added in an amount of 1-3 mols per mol of naphthalene, the recycle of monononylnaphthalene amounting to 0.2-4 parts by weight per part of naphthalene.

Production of conjugated diolefines

Conjugated diolefins and formaldehyde are obtained by heating a 4-alkyl-5,6-dihydro-2H-pyran. This is preferably effected at 300-600 DEG C. in the vapour phase in the presence of steam but the absence of catalysts. An inert solid such as silica gel may be present. The 4-methyl compound produces isoprene. 4-alkyl-5,6-dihydro-2H-pyrans are obtained either by heating a 4-alkyl-4-methyl-1,3-dioxane in the liquid phase in the presence of ferric, zinc, mercuric and/or stannic chloride, or as a by-product in the decomposition of 4,4-dimethyl-1,3-dioxane to form isoprene e.g. over boron phosphate/silica gel.

Improvements in the manufacture and production of aromatic hydrocarbons

... 258,608. I. G. Farbenindustrie Akt.- Ges. Oct. 12,1925, [Convention date]. Aromatic hydrocarbons, mainly of the benzene series, are produced by passing a methane-containing gas at an elevated temperature and pressure over a catalyst comprising a carbonate or other salt of the alkaline earth metals including magnesium and beryllium, or an oxide or hydroxide of magnesium and beryllium, or a compound of selenium, tellurium and thallium, or consisting of active silica or active charcoal or mixtures of these substances with each other or with other materials. Temperatures of 450‹- 800‹ C. are generally employed in conjunction with pressures ranging from 50 to 1000 atmospheres. According to the example, a liquid rich in benzene hydrocarbons is obtained by passing natural gas, which consists chiefly of methane together with ethane, propane and ethylene, at a pressure of 150 atmospheres through a vessel filled with active silica and maintained at a temperature of 600‹ C. The Specification as open ...

Catalytic process of condensation of organic compounds unsaturated and catalyst for its implementation.

Process of aromatic hydrocarbon alkylation.

Process of catalyst regeneration of hydrogenation.

PROCEDURE FOR THE PRODUCTION OF A MODIFIED CRYSTALLINE ONE OF SILICIC ACID MATERIAL

PROCEDURE FOR THE PRODUCTION OF HYDROCARBONS

PROCEDURE FOR THE PRODUCTION OF TERT.OLEFINEN

Procedure for catalytic splitting of Isobutyraldehyd

DIISOBUTYLENVERFAHREN

INCREASE OF THE ACHIEVEMENT OF A MOLECULAR SIEVE

VERFAHREN ZUR HERSTELLUNG EINES MODIFIZIERTEN KRISTALLINEN KIESELSAEUREMATERIALS

PROCEDURE FOR THE PRODUCTION OF ETHYLS

PROCEDURE FOR THE PRODUCTION OF A MODIFIED CRYSTALLINE ONE OF SILICIC ACID MATERIAL

PROCEDURE FOR THE PRODUCTION A ALUMINUM MODEFIZIERTEN OF A SILICIC ACID

PROCEDURE FOR THE PRODUCTION OF TERT.OLEFINEN

ISOPARAFFINOLEFIN ALKYLIERUNGSPROZESS

PROCEDURE FOR THE CATALYTIC DEHYDROGENATION OF ALKYL-AROMATIC HYDROCARBONS

PROCEDURE FOR THE ALKYLATION OF BENZENE OR SUBSTITUTED BENZENE OR FOR TRANSALKYLIERUNG OF ALKYLATED BENZENE

CATALYTICALLY ACTIVE GEL AND PROCEDURE FOR THE PRODUCTION.

PROCEDURE FOR UNSETZUNG FROM BUTADIENE TO STYRENE OR ETHYLBENZOL OR BOTH CATALYSTS CONTAINING WITH USE OF MOLYBDEN

PROCEDURE FOR THE CONVERSION FROM METHANE TO HIGHER HYDROCARBONS

CATALYST COMPOSITION AND PROCEDURE FOR THE TRANSFORMATION OF C3UND C4-KOHLENWASSERSTOFFEN.

AMORPHOUS SILICIC ACID PARTICLES, PROCEDURES FOR THEIR PRODUCTION AND THEIR USE.

PROCEDURE FOR THE PRODUCTION OF ETHYL ETHANGEMI.

PROCEDURE FOR THE OLIGOMERISIERUNG OF LIGHT OLEFINEN.

PROCEDURE FOR THE PRODUCTION OF HYDROCARBONS.

CATALYST PRODUCTION.

Process for producing alkylated aromatic compounds and process for producing phenols

According to a process of the invention, a ketone, an aromatic compound and hydrogen as starting materials are reacted together in a single reaction step to produce an alkylaromatic compound in high yield. A process for producing phenols in the invention includes a step of performing the above alkylation process and does not increase the number of steps compared to the conventional cumene process. The process for producing alkylated aromatic compounds includes reacting an aromatic compound such as benzene, a ketone such as acetone and hydrogen in the presence of a solid acid substance, preferably a zeolite, and a silver-containing catalyst.

Olefin production process

A novel olefin production process is provided which can be established as an industrial and practical process capable of producing olefins by directly reacting a ketone and hydrogen in a single reaction step. In particular, a novel olefin production process is provided in which propylene is obtained with high selectivity by directly reacting acetone and hydrogen. The olefin production process according to the present invention includes reacting a ketone and hydrogen in the presence of at least one dehydration catalyst and a silver-containing catalyst, and the at least one dehydration catalyst is selected from metal oxide catalysts containing a Group 6 element, zeolites, aluminas and heteropoly acid salts in which part or all the protons in heteropoly acids are exchanged with metal cations.

Removal of Hydrogen From Dehydrogenation Processes

A process and system for dehydrogenating certain hydrocarbons is disclosed. The process includes contacting a dehydrogenatable hydrocarbon with steam in the presence of a dehydrogenation catalyst to form hydrogen and a dehydrogenated hydrocarbon. Some of the hydrogen is then removed and some of the remaining dehydrogenatable hydrocarbon is dehydrogenated.

Methane aromatization catalyst, method of making and method of using the catalyst

A catalyst for converting methane to aromatic hydrocarbons is described herein. The catalyst comprises an active metal or a compound thereof, and an inorganic oxide support wherein the active metal is added to the support in the form of metal oxalate. The metal oxalate-derived catalyst exhibits superior performance in the conversion of methane-rich feed to aromatics products relative to catalysts prepared from non-oxalate metal precursors. A method of making the catalyst and a method of using the catalyst are also described.

Methods for removing unsaturated aliphatic hydrocarbons from a hydrocarbon stream using an acidic molecular sieve

Disclosed is a method for removing unsaturated aliphatic compounds from a hydrocarbon feed stream by contacting the hydrocarbon feed stream with an acidic molecular sieve to produce a hydrocarbon effluent stream having a lower unsaturated aliphatic content relative to the hydrocarbon feed stream. The hydrocarbon feed stream comprises an aromatic compound, a nitrogen compound, and an unsaturated aliphatic compound.

Dehydrogenation Process

In a dehydrogenation process a hydrocarbon stream comprising at least one non-aromatic six-membered ring compound and at least one five-membered ring compound is contacted with a first catalyst comprising at least one metal component and at least one support and a second catalyst. The first catalyst is utilized to convert at least a portion of the at least one non-aromatic six-membered ring compound in the hydrocarbon stream to at least one aromatic compound and the second catalyst is utilized to convert at least a portion of the at least one five-membered ring compound in the hydrocarbon stream to at least one paraffin.

Catalyst and process for hydrogenating aromatics

The present invention relates to an eggshell catalyst comprising an active metal selected from the group consisting of ruthenium, rhodium, palladium, platinum and mixtures thereof, applied to a support material comprising silicon dioxide, wherein the pore volume of the support material is 0.6 to 1.0 ml/g, determined by Hg porosimetry, the BET surface area is 280 to 500 m 2 /g, and at least 90% of the pores present have a diameter of 6 to 12 nm, to a process for preparing this eggshell catalyst, to a process for hydrogenating an organic compound which comprises at least one hydrogenatable group using the eggshell catalyst, and to the use of the eggshell catalyst for hydrogenating an organic compound.

Process for preparing an alkene

A process for the preparation of an alkene from an oxygenate comprising contacting a reactant feedstream comprising at least one oxygenate reactant and water with a supported heteropolyacid catalyst at a temperature of at least 170° C., wherein the process is initiated using a start-up procedure comprising the following steps: (i) heating the supported heteropolyacid catalyst to a temperature of at least 220° C.; (ii) maintaining the heat-treated supported heteropolyacid catalyst of step (i) at a temperature of at least 220° C. for a time sufficient to remove bound water from the heteropolyacid component of the supported heteropolyacid catalyst; and (iii) whilst maintaining the supported heteropolyacid catalyst of step (ii) at a temperature of at least 220° C., contacting the supported heteropolyacid catalyst with the reactant feedstream having a temperature of at least 220° C.

Process for the Production of Light Olefins from Synthesis Gas

A new process for light-olefins production is disclosed. The process comprises the step of contacting syngas with a iron-based catalyst at a temperature in the range from 250° C. to 350° C. and at a pressure in the range from 10 bar to 40 bar. By so doing a production of light olefins with a selectivity of at least 80% is obtained.

Production of propylene via simultaneous dehydration and skeletal isomerisation of isobutanol on acid catalysts followed by metathesis

The present invention relates to a process for the production of propylene in which in a first step isobutanol is subjected to a simultaneous dehydration and skeletal isomerisation to make substantially corresponding olefins, having the same number of carbons and consisting essentially of a mixture of n-butenes and iso-butene and in a second step n-butenes are subjected to methathesis, said process comprising: a) introducing in a reactor a stream (A) comprising isobutanol, optionally water, optionally an inert component, b) contacting said stream with a catalyst in said reactor at conditions effective to dehydrate and skeletal isomerase at least a portion of the isobutanol to make a mixture of n-butenes and iso-butene, c) recovering from said reactor a stream (B), removing water, the inert component if any and unconverted isobutanol if any to get a mixture of n-butenes and iso-butene, d) fractionating said mixture to produce a n-butenes stream (N) and to remove the essential part of isobutene optionally recycled with stream (A) to the dehydration/isomerization reactor of step b), e) sending the stream (N) to a methathesis reactor and contacting stream (N) with a catalyst in said methathesis reactor, optionally in the presence of ethylene, at conditions effective to produce propylene, f) recovering from said methathesis reactor a stream (P) comprising essentially propylene, unreacted n-butenes, heavies, optionally unreacted ethylene, g) fractionating stream (P) to recover propylene and optionally recycling unreacted n-butenes and unreacted ethylene to the methathesis reactor.

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

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

Process for making isooctenes from aqueous isobutanol

The present invention relates to a catalytic process for making isooctenes using a reactant comprising isobutanol and water. The isooctenes so produced are useful for the production of fuel additives.

Isomerization of light alpha-olefins to light internal olefins

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

3,3',4,4'-tetraalkyl cyclohexylbenzene and method for producing same

The present invention relates to a 3,3′,4,4′-tetraalkyl cyclohexylbenzene represented by the general formula (1): wherein R represents an alkyl group having 1 to 4 carbon atoms, which may be easily converted into a 3,3′,4,4′-biphenyltetracarboxylic acid and a 3,3′,4,4′-biphenyltetracarboxylic dianhydride thereof, which are a starting material for a polyimide, via a 3,3′,4,4′-tetraalkylbiphenyl; and a method for producing the same.

Catalyst for metathesis of ethylene and 2-butene and/or double bond isomerization

A process for the double-bond isomerization of olefins is disclosed. The process may include contacting a fluid stream comprising olefins with a fixed bed comprising an activated basic metal oxide isomerization catalyst to convert at least a portion of the olefin to its isomer. The isomerization catalysts disclosed herein may have a reduced cycle to cycle deactivation as compared to conventional catalysts, thus maintaining higher activity over the complete catalyst life cycle.

Process for Making Alkylated Aromatic Compound

A process for producing an alkylated aromatic compound comprises contacting an aromatic starting material and hydrogen with a plurality of catalyst particles under hydroalkylation conditions to produce an effluent comprising the alkylated aromatic compound, the catalyst comprising a composite of a solid acid, an inorganic oxide different from the solid acid and a hydrogenation metal, wherein the distribution of the hydrogenation metal in at least 60 wt % of the catalyst particles is such that the average concentration of the hydrogenation metal in the rim portion of a given catalyst particle is Crim, the average concentration of the hydrogenation metal in the center portion of the given catalyst particle is Ccenter, where 0.2≦Crim/Ccenter<2.0. Also disclosed are hydroalkylation catalyst and process for making phenol and/or cyclohexanone using the catalyst.

Catalytic oxidation method and method for producing conjugated diene

An object of the present invention is to suppress performance deterioration of a molybdenum composite oxide-based catalyst at the time of performing gas-phase catalytic partial oxidation with molecular oxygen by using a tubular reactor. The present invention relates to a catalytic oxidation method using a tubular reactor in which a Mo compound layer containing a Mo compound and a composite oxide catalyst layer containing a Mo composite oxide catalyst are arranged in this order from a reaction raw material supply port side and under a flow of a mixed gas containing 75 vol % of air and 25 vol % of water vapor at 440° C., a Mo sublimation amount of the Mo compound is larger than a Mo sublimation amount of the Mo composite oxide catalyst under the same conditions.

CATALYST, AND METHOD FOR DIRECT CONVERSION OF SYNGAS TO PREPARE LIGHT OLEFINS

A process for direct synthesis of light olefins uses syngas as the feed raw material. This catalytic conversion process is conducted in a fixed bed or a moving bed using a composite catalyst containing components A and B (A+B). The active ingredient of catalyst A is metal oxide; and catalyst B is an oxide supported zeolite. A carrier is one or more of AlO, SiO, TiO, ZrO, CeO, MgO and GaOhaving hierarchical pores; the zeolite is one or more of CHA and AEI structures. The loading of the zeolite is 4%-45% wt. A weight ratio of the active ingredients in the catalyst A and the catalyst B is within a range of 0.1-20, and preferably 0.3-5. The total selectivity of the light olefins comprising ethylene, propylene and butylene can reach 50-90%, while the selectivity of a methane byproduct is less than 15%. 1. A catalyst , wherein the catalyst is a composite catalyst composed of A+B; the catalyst component A and the catalyst component B are compounded by mechanical mixing method; the active ingredients of the catalyst component A are active metal oxides; the catalyst component B are supported zeolites; the carrier is at least one of porous AlO , SiO , TiO , ZrO , CeO , MgO and GaO; the zeolite is at least one of CHA and AEI structures; the loading of the zeolite is 4%-45% wt; and the active metal oxide is at least one of MnO , MnCrO , MnAlO , MnZrO , ZnO , ZnCrO , ZnAlO , CoAlOand FeAlO.2. The catalyst according to claim 1 , wherein at least one of porous AlO claim 1 , SiO claim 1 , TiO claim 1 , ZrO claim 1 , CeO claim 1 , MgO and GaOin the catalyst component B is used as the carrier; specific surface area is 30-250 m/g; pore volume is 0.25-0.80 ml/g; through calculation according to the specific surface area claim 1 , mesoporous specific surface area occupies 30-75% and macroporous specific surface area occupies 25-70%; and the zeolite is used as an active component and dispersed on the carrier by in situ growth or physical mixing mode.3. The catalyst according to claim 1 , ...

PROPYLENE PRODUCTION USING A MESOPOROUS SILICA FOAM METATHESIS CATALYST

Embodiments of a metathesis process for producing propylene comprise providing a metathesis catalyst comprising an amorphous mesoporous silica foam impregnated with metal oxides, where the metathesis catalyst has a pore size distribution of at least 3 nm to 40 nm and a total pore volume of at least 0.700 cm/g. The process further involves producing a product stream comprising propylene by contacting a feed stream comprising butene with the metathesis catalyst. 1. A metathesis process for producing propylene comprising:{'sup': '3', 'providing a metathesis catalyst comprising an amorphous mesoporous silica foam impregnated with metal oxides, where the metathesis catalyst has a pore size distribution of at least 3 nm to 40 nm and a total pore volume of at least 0.700 cm/g; and'}producing a product stream comprising propylene by contacting a feed stream comprising butene with the metathesis catalyst.2. The process of further comprising tri-block copolymer structuring agent claim 1 , where the tri-block copolymer structuring agent is poly(ethylene glycol)-block-poly(propylene glycol)-block-poly(ethylene glycol) structure.3. The process of where the metathesis catalyst catalyzes isomerization of 2-butene to 1-butene followed by cross-metathesis of 2-butene and 1-butene into a metathesis product stream comprising propylene4. The process of where at least 90% of the 2-butene is converted to 1-butene via isomerization.5. The process of where the pore size distribution is from at least 4 nm to 10 nm and the total pore volume is from at least 0.800 cm/g to 1.5 cm/g.6. The process of where the metathesis catalyst has a total acidity from 0.125 mmol/g to 0.500 mmol/g claim 1 , and a surface area of 400 to 500 m/g.7. The process of where the metal oxide is an oxide of molybdenum claim 1 , rhenium claim 1 , tungsten claim 1 , or combinations thereof.8. The process of where the metal oxide is tungsten oxide.9. The process of where the metathesis catalyst has a molar ratio for ...

SYSTEMS AND METHODS FOR PRODUCING PROPYLENE

According to one embodiment described in this disclosure, a process for producing propylene may comprise at least partially metathesizing a first stream comprising at least about 10 wt. % butene to form a metathesis-reaction product, at least partially cracking the metathesis-reaction product to form a cracking-reaction product comprising propylene, and at least partially separating propylene from the cracking-reaction product to form a product stream comprising at least about 80 wt. % propylene. 1. A process for producing propylene , the process comprising:{'sup': '3', 'at least partially metathesizing a first composition comprising at least 10 wt. % butene to form a metathesis-reaction product, where the first composition is metathesized with a metathesis catalyst comprising a mesoporous silica catalyst impregnated with metal oxide, where the mesoporous silica catalyst includes a pore size distribution of about 2.5 nm to about 40 nm and a total pore volume of at least about 0.600 cm/g;'}at least partially cracking the metathesis-reaction product to form a cracking-reaction product comprising propylene, where the metathesis-reaction product is cracked with a cracking catalyst comprising a mordenite framework inverted (MFI) structured silica catalyst, where the MFI structured silica catalyst includes total acidity of 0.001 mmol/g to 0.1 mmol/g; andat least partially separating propylene from the cracking-reaction product to form a product composition comprising at least 80 wt. % propylene.2. The process of claim 1 , where the MFI structured silica catalyst has a pore size distribution of at least 1.5 nm to 3 nm.3. The process of claim 1 , where the MFI structured silica catalyst is free of acidity modifiers selected from the group consisting of rare earth modifiers claim 1 , phosphorus modifiers claim 1 , potassium modifiers claim 1 , and combinations thereof.4. The process of claim 1 , where the metathesis catalyst is positioned generally upstream of the cracking ...

DUAL CATALYST SYSTEM FOR PROPYLENE PRODUCTION

Embodiments of processes for producing propylene utilize a dual catalyst system comprising a mesoporous silica catalyst impregnated with metal oxide and a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm/g, and the MFI structured silica catalyst has a total acidity of 0.001 mmol/g to 0.1 mmol/g. The propylene is produced from the butene stream via metathesis by contacting the mesoporous silica catalyst and subsequent cracking by contacting the MFI structured silica catalyst. 1. A process for production of propylene comprising: [{'sup': '3', 'a mesoporous silica catalyst impregnated with metal oxide, where the mesoporous silica catalyst includes a pore size distribution of about 2.5 nm to about 40 nm and a total pore volume of at least about 0.600 cm/g, and'}, 'a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the MFI structured silica catalyst includes a total acidity of 0.001 mmol/g to 0.1 mmol/g,, 'providing a dual catalyst system comprisingproducing propylene from a stream comprising butene via metathesis and cracking by contacting the stream comprising butene with the dual catalyst system, where the stream comprising butene contacts the mesoporous silica catalyst before contacting the MFI structured silica catalyst.2. The process of where the MFI structured silica catalyst has a pore size distribution of at least 1.5 nm to 3 nm.3. The process of where the MFI structured silica catalyst is free of acidity modifiers selected from the group consisting of rare earth modifiers claim 1 , phosphorus modifiers claim 1 , potassium modifiers claim 1 , and combinations thereof.4. The process of where the mesoporous silica catalyst catalyzes isomerization of 2-butene to 1-butene followed by cross-metathesis of ...

Systems and methods for producing propylene

According to one or more embodiments described herein, a process for producing propylene, the process comprising at least partially metathesizing a first portion of a first stream to form a first metathesis-reaction product, at least partially cracking the first metathesis-reaction product to form a cracking-reaction product, the cracking reaction product comprising propylene and ethylene, at least partially separating ethylene from at least the cracking reaction product to form a first recycle stream, combining the first recycle stream with a second portion of the first stream to a form a mixed stream, and at least partially metathesizing the mixed stream to from a second metathesis-reaction product. In embodiments, the second metathesis-reaction product may comprise propylene, the first stream may comprise butene, and the first recycle stream may comprise ethylene.

Process for Converting Butanol into Propylene

Process for selective the conversion of primary C4 alcohol into propylene comprising: contacting a stream () containing essentially a primary C4 alcohol with at least one catalyst at a temperature ranging from 150° C. to 500° C. and at pressure ranging from 0.01 MPa to 10 MPa conditions effective to transform said primary C4 alcohol into an effluent stream () containing essentially propylene, carbon monoxide and di-hydrogen, said transformation of primary C4 alcohol comprising at least a reaction of decarbonylation and optionally a decarboxylation reaction, said at least one catalyst comprising a support being a non-acidic i.e. having a TPD NH3 of less than 50 preferably less than 40 μmol/g and optionally a non-basic catalyst i.e. having a TPD CO2 of less than 100 preferably less than 50 μmol/g. 115.-. (canceled)16. A process for the conversion of primary C4 alcohol into propylene comprising:{'b': 1', '2', '5, 'contacting a stream () containing a primary C4 alcohol with at least one catalyst at a temperature ranging from 150° C. to 500° C. and at pressure ranging from 0.01 MPa to 10 MPa to transform the primary C4 alcohol into an effluent stream (, ) containing propylene, carbon monoxide and di-hydrogen, the transformation of primary C4 alcohol comprising at least a reaction of decarbonylation and optionally a decarboxylation reaction, the at least one catalyst comprising support which is non-acidic, having a TPD NH3 of less than 50 μmol/g and which is also a non-basic, having a TPD CO2 of less than 100 μmol/g.'}17125. The process according to wherein stream () is contacted with the at least one catalyst to produce an effluent stream ( claim 16 , ) wherein at least 1 wt % of primary C4 alcohol is converted into propylene claim 16 , carbon monoxide and di-hydrogen.181121. The process according to claim 16 , wherein the step of contacting the primary C4 alcohol stream () with the at least one catalyst is performed in a single reaction zone (A) and the at least one ...

PROCESS FOR MAKING STYRENE USING MICROCHANNEL PROCESS TECHNOLOGY

The disclosed invention relates to a process for converting ethylbenzene to styrene, comprising: flowing a feed composition comprising ethylbenzene in at least one process microchannel in contact with at least one catalyst to dehydrogenate the ethylbenzene and form a product comprising styrene; exchanging heat between the process microchannel and at least one heat exchange channel in thermal contact with the process microchannel; and removing product from the process microchannel. Also disclosed is an apparatus comprising a process microchannel, a heat exchange channel, and a heat transfer wall positioned between the process microchannel and heat exchange channel wherein the heat transfer wall comprises a thermal resistance layer. 1178-. (canceled)179. An apparatus , comprising:a process microchannel;a heat exchange channel; anda heat transfer wall positioned between the process microchannel and the heat exchange channel, the heat transfer wall comprising at least one thermal resistance layer.180. The apparatus of wherein the thermal resistance layer is positioned on the heat transfer wall and/or embedded within the heat transfer wall.181. The apparatus of wherein the thermal resistance layer comprises a vacuum claim 179 , a gaseous material claim 179 , a liquid and/or a solid material.182. The apparatus of wherein the thermal resistance layer comprises a solid material which contains void spaces claim 179 , openings and/or through holes.183. The apparatus of wherein the thermal resistance layer comprises one or more strips or shims which contain void spaces claim 179 , openings and/or through holes.184. The apparatus of wherein the thermal resistance layer comprises one or more strips with grooves formed in the strip.185. The apparatus of wherein the thermal resistance layer comprises one or more shims claim 179 , each of the shims having a first surface and a second surface claim 179 , and grooves formed in the first surface and/or the second surface.186. The ...

CATALYST AND METHOD FOR AROMATIZATION OF C3-C4 GASES, LIGHT HYDROCARBON FRACTIONS AND ALIPHATIC ALCOHOLS, AS WELL AS MIXTURES THEREOF

The invention relates to hydrocarbon feedstock processing technology, in particular, to catalysts and technology for aromatization of C-Chydrocarbon gases, light low-octane hydrocarbon fractions and oxygen-containing compounds (C-Caliphatic alcohols), as well as mixtures thereof resulting in producing an aromatic hydrocarbon concentrate (AHCC). The catalyst comprises a mechanical mixture of 2 zeolites, one of which is characterized by the silica/alumina ratio SiO/AlO=20, pre-treated with an aqueous alkali solution and modified with oxides of rare-earth elements used in the amount from 0.5 to 2.0 wt % based on the weight of the first zeolite. The second zeolite is characterized by the silica/alumina ratio SiO/AlO═82, comprises sodium oxide residual amounts of 0.04 wt % based on the weight of the second zeolite, and is modified with magnesium oxide in the amount from 0.5 to 5.0 wt % based on the weight of the second zeolite. Furthermore, the zeolites are used in the weight ratio from 1.7:1 to 2.8:1, wherein a binder comprises at least silicon oxide and is used in the amount from 20 to 25 wt % based on the weight of the catalyst. The process is carried out using the proposed catalyst in an isothermal reactor without recirculation of gases from a separation stage, by contacting a fixed catalyst bed with a gaseous feedstock, which was evaporated and heated in a preheater. The technical result consists in achieving a higher aromatic hydrocarbon yield while ensuring almost complete conversion of the HC feedstock and oxygenates, an increased selectivity with respect to forming xylols as part of an AHCC, while simultaneously simplifying the technological setup of the process by virtue of using a reduced (inter alia, atmospheric) pressure. 14-. (canceled)5. A catalyst for the aromatization of mixtures of hydrocarbons and aliphatic alcohols , the catalyst comprising: a mixture of a first pentasil zeolite and a second pentasil zeolite; the first pentasil zeolite comprising a ...

PROCESS FOR DEHYDRATION OF OXYGENATES WITH HETEROPOLYACID CATALYSTS HAVING MIXED OXIDE SUPPORTS AND USE OF THE SAME

The present invention relates to a process for producing ethene by the vapour phase dehydration of ethanol using a supported heteropolyacid catalyst. In particular, the present invention involves the use of a supported heteropolyacid catalyst, wherein the supported heteropolyacid catalyst is: i) a mixed oxide support comprising silica and a transition metal oxide, wherein silica is present in an amount of at least 50 wt. %, based on the weight of the mixed oxide support; or ii) a mixed oxide support comprising zirconia and a different transition metal oxide, wherein zirconia is present in an amount of at least 50 wt. %, based on the weight of the mixed oxide support. When used in a process for the preparation of ethene by vapour phase dehydration, and after attaining steady-state performance of the catalyst, the process may be operated continuously with the same supported heteropolyacid catalyst for at least 150 hours without any regeneration of the catalyst. 1. A process for the vapour phase chemical dehydration of ethanol in a reactor in the presence of a supported heteropolyacid catalyst , wherein the support of the supported heteropolyacid catalyst is: i) a mixed oxide support comprising silica and a transition metal oxide , wherein silica is present in an amount of at least 50 wt. % , based on the weight of the mixed oxide support; or ii) a mixed oxide support comprising zirconia and a different transition metal oxide , wherein zirconia is present in an amount of at least 50 wt. % , based on the weight of the mixed oxide support; and wherein , after attaining steady-state performance of the catalyst , said process is operated continuously with the same supported heteropolyacid catalyst for at least 150 hours , without any regeneration of the catalyst.2. A process according to claim 1 , wherein claim 1 , after attaining steady-state performance of the catalyst claim 1 , the process is operated continuously with the same supported heteropolyacid catalyst for at ...

CATALYSTS FOR PETROCHEMICAL CATALYSIS

Metal oxide catalysts comprising various dopants are provided. The catalysts are useful as heterogeneous catalysts in a variety of catalytic reactions, for example, the oxidative coupling of methane to C2 hydrocarbons such as ethane and ethylene. Related methods for use and manufacture of the same are also disclosed. 185-. (canceled)86. A method for the oxidative coupling of methane , the method comprising contacting methane with a catalyst at temperatures ranging from about 550° C. to about 750° C. , wherein the method comprises a methane conversion of greater than 20% and a C2 selectivity of greater than 50% , and wherein the catalyst comprises the following formula:{'br': None, 'sub': x', 'y', 'z, 'ABO;'} A is an element from the lanthanides or group 2, 3, 4, 6 or 13;', 'B is an element from groups 4, 12 or 13 of the periodic table or Ce, Pr, Nd, Sm, Eu, Gd, Tb or Ho;', 'O is an oxygen anion; and', 'x, y and z are each independently numbers greater than 0,, 'whereinthe catalyst further comprising one or more dopants from any one of groups 2, 3 or the lanthanides, and provided that A and B are not the same.87. The method of claim 86 , wherein A is Ba claim 86 , Zr claim 86 , Sr claim 86 , Sm claim 86 , Hf claim 86 , Gd claim 86 , Er claim 86 , Y claim 86 , Ca claim 86 , La claim 86 , Mg claim 86 , W claim 86 , B claim 86 , Tb or Ce.88. The method of claim 86 , wherein B is Zn claim 86 , Hf claim 86 , Zr claim 86 , Al claim 86 , Ti claim 86 , Pr claim 86 , Nd claim 86 , Ce claim 86 , Sm claim 86 , Eu claim 86 , Gd claim 86 , Tb or Ho.89. The method of claim 86 , wherein A is from group 2 claim 86 , and B is from group 4.90. The method of claim 86 , wherein A is Ba claim 86 , Sr or Ca.91. The method of claim 86 , wherein B is Ti claim 86 , Zr or Hf.92. The method of claim 86 , wherein the catalyst has the formula ABO.93. The method of claim 86 , wherein the catalyst comprises one or more dopant from group 2.94. The method of claim 86 , wherein the catalyst comprises ...

Silver Promoted Catalysts for Oxidative Coupling of Methane

An oxidative coupling of methane (OCM) catalyst composition comprising one or more oxides doped with Ag; wherein one or more oxides comprises a single metal oxide, mixtures of single metal oxides, a mixed metal oxide, mixtures of mixed metal oxides, or combinations thereof; and wherein one or more oxides is not LaOalone. A method of making an OCM catalyst composition comprising calcining one or more oxides and/or oxide precursors to form one or more calcined oxides, wherein the one or more oxides comprises a single metal oxide, mixtures of single metal oxides, a mixed metal oxide, mixtures of mixed metal oxides, or combinations thereof, wherein the one or more oxides is not LaOalone, and wherein the oxide precursors comprise oxides, nitrates, carbonates, hydroxides, or combinations thereof; doping the one or more calcined oxides with Ag to form the OCM catalyst composition; and thermally treating the OCM catalyst composition. 1. An oxidative coupling of methane (OCM) catalyst composition doped with silver (Ag).2. The OCM catalyst composition of claim 1 , wherein the OCM catalyst composition comprises one or more oxides doped with silver (Ag); wherein the one or more oxides comprises a single metal oxide claim 1 , mixtures of single metal oxides claim 1 , a mixed metal oxide claim 1 , mixtures of mixed metal oxides claim 1 , or combinations thereof; and wherein the one or more oxides is not LaOalone.3. The OCM catalyst composition of claim 2 , wherein the single metal oxide comprises one metal cation selected from the group consisting of alkali metal cations claim 2 , alkaline earth metal cations claim 2 , rare earth element cations claim 2 , and cations of elements that can form oxides with redox properties.4. The OCM catalyst composition of claim 2 , wherein the mixed metal oxide comprises two or more different metal cations claim 2 , wherein each metal cation can be independently selected from the group consisting of alkali metal cations claim 2 , alkaline earth ...

METHOD OF TREATING BUTENE TO FORM PROPYLENE/ETHYLENE MIXTURE

A method of producing propylene and ethylene from a butene-containing hydrocarbon stream by cracking olefin compounds in the butene-containing hydrocarbon stream in the presence of a core-shell ZSM catalyst, wherein the core-shell ZSM catalyst comprises a ZSM-5 core and a silica shell disposed thereon. Various embodiments of the method of producing propylene and ethylene, and the method of making the core-shell ZSM catalyst are also provided. 1. A method of treating butene to form a mixture of propylene and ethylene , comprising:contacting a butene-containing hydrocarbon stream with a core-shell ZSM catalyst in a fixed-bed reactor to form a product stream comprising propylene and ethylene, wherein the core-shell ZSM catalyst is present in the fixed bed reactor as particles having a diameter of 0.5-1.0 mm packed in the fixed bed reactor,wherein at least 50 wt % of the butene-containing hydrocarbon stream is butene, andwherein the core-shell ZSM catalyst comprises:a ZSM-5 core, anda silica shell having a thickness in the range of 0.5 to 50 μm, which covers at least a portion of a surface of the ZSM-5 core.25-. (canceled)6. The method of claim 1 , wherein at least 50 wt % of the product stream is propylene and ethylene.7. The method of claim 1 , wherein a propylene-to-ethylene weight ratio of the product stream is within the range of 0.2 to 4.8. The method of claim 1 , further comprising:treating the core-shell ZSM catalyst with nitrogen at a temperature in the range of 400 to 700° C. prior to the contacting.9. The method of . further comprising:mixing the butene-containing hydrocarbon stream with nitrogen to form a gaseous mixture prior to the contacting, wherein a partial pressure of the butene-containing hydrocarbon stream in the gaseous mixture is within the range of 5 to 50 psi.10. The method of claim 1 , wherein the butene-containing hydrocarbon stream is contacted with the core-shell ZSM catalyst at a temperature in the range of 400 to 700° C. claim 1 , and a ...

METHOD FOR MAKING A CATALYST AND CRACKING A HYDROCARBON STREAM TO FORM PROPYLENE/ETHYLENE

A method of producing propylene and ethylene from a butene-containing hydrocarbon stream by cracking olefin compounds in the butene-containing hydrocarbon stream in the presence of a core-shell ZSM catalyst, wherein the core-shell ZSM catalyst comprises a ZSM-5 core and a silica shell disposed thereon. Various embodiments of the method of producing propylene and ethylene, and the method of making the core-shell ZSM catalyst are also provided. 1. A method for making a catalyst and cracking a hydrocarbon stream to form propylene and ethylene , comprising:mixing a ZSM silicalite with a silicalite gel to form a silicalite mixture, hydrothermally treating the silicalite mixture then calcining to form a core-shell ZSM catalyst.contacting a butene-containing hydrocarbon stream with the core-shell ZSM catalyst in a fixed-bed reactor to form a product stream comprising propylene and ethylene,wherein at least 50 wt % of the butene-containing hydrocarbon stream is butene, and a ZSM-5 core, and', 'a silica shell having a thickness in the range of 0.5 to 50 μm, which covers at least a portion of a surface of the ZSM-5 core., 'wherein the core-shell ZSM catalyst comprises2. The method of claim 1 , wherein the silica shell has a thickness in the range of 0.5 to 30 μm.3. The method of claim 1 , wherein the core-shell ZSM catalyst is dispersed in a silica and/or an alumina binder.4. The method of claim 1 , wherein a weight percent of the silica shell in the core-shell ZSM catalyst is within the range of 4 to 75 wt % claim 1 , with the weight percent being relative to the total weight of the core-shell ZSM catalyst.5. The method of claim 1 , wherein the core-shell ZSM catalyst has an acidity of less than 0.1 mmol/g.6. The method of claim 1 , wherein at least 50 wt % of the product stream is propylene and ethylene.7. The method of claim 1 , wherein a propylene-to-ethylene weight ratio of the product stream is within the range of 0.2 to 4.8. The method of claim 1 , further comprising: ...

Method for producing conjugated diolefin

A method for producing a conjugated diolefin is configured as follows. A monoolefin having four or more carbon atoms is fed from a monoolefin feed nozzle(s) installed at n place(s) (n=1, 2, . . . , n). In addition, at least 50% or more of a total amount of an oxygen-containing gas is fed from an oxygen-containing gas feed nozzle located at a bottom of a fluidized bed reactor. Furthermore, the monoolefin feed nozzles at distances a1, a2, . . . , an from the oxygen-containing gas feed nozzle feed the monoolefin having four or more carbon atoms at ratios of b1, b2, . . . , bn (b1+b2+ . . . +bn=1), respectively, and an arithmetic mean value represented by the following formula and obtained from the above distances and the above ratios is 100 mm or more. arithmetic mean value= a 1* b 1+ a 2* b 2+ . . . + an*bn

OLEFIN CONVERSION PROCESS

A process for the production of Colefins, which may include: contacting a hydrocarbon mixture comprising alpha-pentenes with an isomerization catalyst to form an isomerization product comprising beta-pentenes; contacting ethylene and the beta-pentenes with a first metathesis catalyst to form a first metathesis product comprising butenes and propylene, as well as any unreacted ethylene and Colefins; and fractionating the first metathesis product to for an ethylene fraction, a propylene fraction, a butene fraction, and a Cfraction. 1. A system for the production of Colefins , the system comprising:an isomerization reaction zone for contacting a hydrocarbon mixture comprising alpha-pentenes with an isomerization catalyst to form an isomerization product comprising beta-pentenes;{'sub': '5', 'a first metathesis reaction zone for contacting ethylene and the beta-pentenes with a first metathesis catalyst to form a first metathesis product comprising butenes and propylene, as well as any unreacted ethylene and Colefins;'}{'sub': '5', 'a separation system for fractionating the first metathesis product to form an ethylene fraction, a propylene fraction, a butene fraction, and a Cfraction; and'}a second metathesis reaction zone for contacting the propylene with a second metathesis catalyst, which may be the same or different than the first metathesis catalyst, to convert at least a portion of the propylene to ethylene and 2-butene and form a second metathesis product.2. The system of claim 1 , further comprising a flow conduit for feeding the first metathesis product and the second metathesis product to a common fractionation system.3. The system of claim 2 , further comprising a flow conduit for withdrawing a propylene product stream.4. The system of claim 3 , further comprising a control system for adjusting a rate of withdrawing the propylene product stream to produce a selected ratio of butene to propylene product.5. The system of claim 1 , further comprising one or more ...

Processes for producing polymer grade light olefins from mixed alcohols

Processes for providing a high purity olefin product are described. The processes involve dehydrating a feedstream comprising a mixture of alcohols having 3 to 8 carbon atoms and forming a mixed olefin stream and a water stream, the mixed olefin stream comprising a mixture of olefins having 3 to 8 carbon atoms. The mixed olefin stream is separated into at least a C 3 olefin stream comprising olefins having 3 carbon atoms and a C 4-8 olefin stream comprising olefins having 4 to 8 carbon atoms. The C 4-8 olefin stream is separated into a C 4 olefin stream comprising olefins having 4 carbon atoms and a C 5-8 olefin stream comprising olefins having 5 to 8 carbon atoms. At least one of the C 3 olefin stream and the C 4 olefin stream is purified.

METHOD OF MAKING AND SEPARATING A PROPYLENE/ETHYLENE MIXTURE FROM BUTENE

A method of producing propylene and ethylene from a butene-containing hydrocarbon stream by cracking olefin compounds in the butene-containing hydrocarbon stream in the presence of a core-shell ZSM catalyst, wherein the core-shell ZSM catalyst comprises a ZSM-5 core and a silica shell disposed thereon. Various embodiments of the method of producing propylene and ethylene, and the method of making the core-shell ZSM catalyst are also provided. 1: A fluidized-bed method of cracking butene to form propylene and ethylene , comprising:contacting a butene-containing hydrocarbon stream with a core-shell ZSM catalyst in a fluidized-bed reactor to form a product stream comprising propylene and ethylene, thenseparating the propylene and ethylene from the product stream with a stripping column,wherein at least 50 wt % of the butene-containing hydrocarbon stream is butene, andwherein the core-shell ZSM catalyst comprises:a ZSM-5 core, anda silica shell having a thickness in the range of 0.5 to 50 μm, which covers at least a portion of a surface of the ZSM-5 core.24-. (canceled)5: The method of claim 1 , wherein the core-shell ZSM catalyst has an acidity of less than 0.1 mmol/g.6: The method of claim 1 , wherein at least 50 wt % of the product stream is propylene and ethylene.7: The method of claim 1 , wherein a propylene-to-ethylene weight ratio of the product stream is within the range of 0.2 to 4.8: The method of claim 1 , further comprising:treating the core-shell ZSM catalyst with nitrogen at a temperature in the range of 400 to 700° C. prior to the contacting.9: The method of claim 1 , further comprising:mixing the butene-containing hydrocarbon stream with nitrogen to form a gaseous mixture prior to the contacting, wherein a partial pressure of the butene-containing hydrocarbon stream in the gaseous mixture is within the range of 5 to 50 psi.10: The method of claim 1 , wherein the butene-containing hydrocarbon stream is contacted with the core-shell ZSM catalyst at a ...

SUPPORTED BIMETALLIC CORE-SHELL STRUCTURE CATALYST AND ITS PREPARATION METHOD

The purpose of the invention is to provide a supported bimetallic core-shell structure catalyst and its preparation method. Supporter, metal salt and reducing agent solution are mixed to synthesize the catalyst M@PdM/ZT by using a one-step synthesis method, wherein the active metal particle M@PdM as core-shell structure, M Is the core representing one of the Ag, Pt, Au and Ir. ZT is the supporter, representing one of hydrotalcite (MgAl-LDH), alumina (AlO) and silica (SiO). By changing the temperature and the reaction time to control the kinetic behavior of the reduction of two kinds of metal ions to realize the construction of core-shell structure. Active metal particle composition and shell thickness are regulated by controlling metal ion concentration. The bimetallic core-shell catalyst prepared by this method showed excellent selectivity and stability in acetylene selective hydrogenation and anthraquinone hydrogenation. 1. A preparation method of supported bimetallic core-shell catalyst comprising:{'sub': 3', '6', '5', '7', '2', '2', '2', '6', '2', '5', '7', '2', '3', '4', '2', '2', '3', '2', '5', '7', '2', '2', '3', '2', '2', '3', '2, 'adding M salt and Pd salt to a reducing solution to obtain a mixed salt solution after ultrasonic irradiation for 4-5 min; wherein a total concentration of M and Pd ions is 0.01-20 mmol/L, a molar ratio of M:Pd ions is 0.1 to 10; M is one of Ag, Pt, Au and Ir; M salt is one of AgNO, HPtCl, Pt(CHO), HIrCl.6HO, Ir(CHO)and HAuCl.4HO; Pd salt is one of the PdCl, Pd(NO), Pd(CHO), Pd(CHCOO); the reducing solution is a mixture of reducing agent and deionized water, wherein, a mass ratio of the deionized water is 0-20%; the reducing agent is one of ethylene glycol, isopropanol, N, n-dimethyl acetamide, N, n-dimethyl formamide and glyceraldehyde; stirring and heating the mixed salt solution for 10-30 min under 40-50° C., adding a supporter and continuing to stir for 10-20min; raising temperature to 100-160° C. and keeping the temperature ...

METHOD OF PREPARING SILICA SUPPORTED CoMoS HYDRODESULFURIZATION CATALYSTS

A method of preparing hydrodesulfurization catalysts having cobalt and molybdenum sulfide deposited on a support material containing mesoporous silica. The method utilizes a sulfur-containing silane that dually functions as a silica source and a sulfur precursor. The method involves an one-pot strategy for hydrothermal treatment and a single-step calcination and sulfidation procedure. The application of the hydrodesulfurization catalysts in treating a hydrocarbon feedstock containing sulfur compounds to produce a desulfurized hydrocarbon stream is also specified. 1: A method of preparing a CoMoS hydrodesulfurization catalyst , the method comprising:mixing a molybdenum precursor, a cobalt precursor, a mercaptoalkyltrialkoxysilane, a structural directing surfactant, an acid, and a solvent to form a reaction mixture;hydrothermally treating the reaction mixture to form a dried mass; andcalcining the dried mass in an activation gas thereby forming the CoMoS hydrodesulfurization catalyst,wherein:the activation gas is at least one selected from the group consisting of air, argon, nitrogen, helium, hydrogen, and carbon monoxide; andthe CoMoS hydrodesulfurization catalyst comprises cobalt and molybdenum sulfide disposed on a support material comprising a mesoporous silica.2: The method of claim 1 , wherein the CoMoS hydrodesulfurization catalyst is not subjected to a sulfidation with a sulfidation reagent.3: The method of claim 1 , wherein the mercaptoalkyltrialkoxysilane is at least one selected from the group consisting of (mercaptomethyl)trimethoxysilane claim 1 , (mercaptomethyl)triethoxysilane claim 1 , (mercaptomethyl)tripropoxysilane claim 1 , (2-mercaptoethyl)trimethoxysilane claim 1 , (2-mercaptoethyl)triethoxysilane claim 1 , (2-mercaptoethyl)tripropoxysilane claim 1 , (3-mercaptopropyl)trimethoxysilane claim 1 , (3-mercaptopropyl)triethoxysilane claim 1 , and (3-mercaptopropyl)tripropoxysilane.4: The method of claim 3 , wherein the mercaptoalkyltrialkoxysilane is ...

METHOD FOR PRODUCING ACRYLONITRILE

The invention relates to a method for producing acrylonitrile which includes a vapor phase catalytic ammoxidation process of performing vapor phase catalytic ammoxidation by bringing a source gas containing propylene, molecular oxygen, and ammonia into contact with a fluidized bed catalyst to obtain acrylonitrile. The method is characterized in that the fluidized bed catalyst consists of particles containing Fe, Sb, and Te, and the vapor phase catalytic ammoxidation process is performed while maintaining a B/A in the range of 2.0 to 5.0, where A denotes an atomic ratio of Te/Sb in a bulk composition of the fluidized bed catalyst and B denotes an atomic ratio of Te/Sb in a surface composition of the particles of the fluidized bed catalyst. According to the method for producing acrylonitrile of the invention, it is possible to stably maintain a high acrylonitrile yield over a long period of time. 1. A method for producing acrylonitrile , the method comprising a vapor phase catalytic ammoxidation process of performing a vapor phase catalytic ammoxidation by bringing a source gas containing propylene , molecular oxygen , and ammonia into contact with a fluidized bed catalyst to obtain acrylonitrile ,wherein the fluidized bed catalyst consists of particles containing Fe, Sb, and Te, andthe vapor phase catalytic ammoxidation process is performed while maintaining a B/A in the range of 2.0 to 5.0, where A denotes an atomic ratio of Te/Sb in a bulk composition of the fluidized bed catalyst and B denotes an atomic ratio of Te/Sb in a surface composition of the particles of the fluidized bed catalyst.2. The method for producing acrylonitrile according to claim 1 , wherein the bulk composition of the fluidized bed catalyst is represented by the following Formula (1).{'br': None, 'sub': 10', 'a', 'b', 'c', 'd', 'e', 'x', '2', 'y, 'FeSbATeDEO.(SiO)\u2003\u2003(1)'}{'sub': '2', '(in Formula (1), Fe, Sb, Te, O, and SiOrepresent iron, antimony, tellurium, oxygen, and silica, ...

LEWIS ACID CATALYSTS FOR PRODUCING TOLUENE AND METHOD FOR MANUFACTURING TOLUENE USING THE SAME

Disclosed is a Lewis acid catalyst for preparation of toluene from 2-methylfuran and a method for preparing toluene from 2-methylfuran by using the same. The catalyst is a zeolite catalyst ion-exchanged with a metal or a metal halide catalyst. The catalyst accelerates the cycloaddition of 2-methylfuran with ethylene and inhibits oligomerization as a side reaction, and thus allows production of toluene from 2-methylfuran with high yield and high selectivity. 1. A catalyst for use in the preparation of toluene from 2-methylfuran ,wherein the catalyst is a Lewis acid catalyst; andwherein the catalyst is a zeolite catalyst ion-exchanged with at least one metal.2. The catalyst for use in the preparation of toluene according to claim 1 , wherein the zeolite catalyst is ion-exchanged with at least one metal selected from the group consisting of alkali metals claim 1 , transition metals and post-transition metals.3. The catalyst for use in the preparation of toluene according to claim 2 , wherein the zeolite catalyst is ion-exchanged with at least one alkali metal.4. The catalyst for use in the preparation of toluene according to claim 3 , wherein the zeolite catalyst is ion-exchanged with Li or Na.5. The catalyst for use in the preparation of toluene according to claim 1 , wherein the zeolite catalyst is a Y-zeolite catalyst having an FAU structure.6. A catalyst for use in the preparation of toluene from 2-methylfuran claim 1 ,wherein the catalyst is a Lewis acid catalyst; andwherein the catalyst is a metal halide catalyst.7. The catalyst for use in the preparation of toluene according to claim 6 , wherein the metal halide catalyst comprises: at least one cation selected from the group consisting of transition metals and post-transition metals; and at least one halogen anion.8. The catalyst for use in the preparation of toluene according to claim 7 , wherein the metal halide catalyst is a metal chloride.9. The catalyst for use in the preparation of toluene according to ...

CATALYST COMPOSITION AND METHOD OF PREPARING POLYOLEFIN USING THE SAME

Provided are a catalyst composition and a method of oligomerizing olefins using the same. When the catalyst composition according to the present invention is used, oligomerization and copolymerization of olefin monomers may be performed in a single reactor at the same time with high efficiency without a separate process of preparing alpha-olefin. Therefore, costs for preparing or purchasing comonomers which are expensive raw materials may be reduced, thereby reducing the production cost of a final product. Contents of SCB (short chain branch) and LCB (long chain branch) in the polyolefin may be increased without separate feeding of comonomers, thereby producing high-quality linear low-density polyethylene. 4. The catalyst composition of claim 1 , wherein Rto Rof the Chemical Formula 1 are phenyl.7. The catalyst composition of claim 1 , wherein the first and second supported catalysts further include each independently the same or different one or more cocatalysts of an aluminum-containing first cocatalyst of the following Chemical Formula 8 and a borate-based second cocatalyst of the following Chemical Formula 9:{'br': None, 'sub': 26', 'k, '—[Al(R)—O]—\u2003\u2003[Chemical Formula 8]'}{'sub': '26', 'claim-text': {'br': None, 'sup': +', '−, 'sub': '4', 'T[BG]\u2003\u2003[Chemical Formula 9]'}, 'wherein Ris the same as or different from each other, and each independently a halogen radical, a hydrocarbyl radical having 1 to 20 carbon atoms, or a hydrocarbyl radical having 1 to 20 carbon atoms, which is substituted with halogen, and k is an integer of 2 or more,'}{'sup': '+', 'wherein T is a polyatomic ion having a valence of +1, B is boron in +3 oxidation state, and Gs are each independently selected from the group consisting of a hydride group, a dialkylamido group, a halide group, an alkoxide group, an aryloxide group, a hydrocarbyl group, a halocarbyl group, and a halo-substituted hydrocarbyl group, and G has 20 or less carbon atoms, provided that G is a halide ...

Polyoxometalates Comprising Noble Metals and Corresponding Metal Clusters

The invention relates to poly oxometalates represented by the formula (A){M′[M″MXORH]} or solvates thereof, corresponding supported poly-oxometalates, and processes for their preparation, as well as corresponding metal-clusters, optionally in the form of a dispersion in a liquid carrier medium or immobilized on a solid support, and processes for their preparation, as well as their use in reductive conversion of organic substrate. 118.-. (canceled)20. The composition of claim 19 , wherein all M′ are the same claim 19 , and all M′ are different from M;wherein M is Pd, M′ is Ag, X is P, and s is 4 or 5; andwherein z and q are 0.21. The composition of claim 19 ,wherein said substituent group R bonded to X via a carbon atom of said substituent group is selected from the group consisting of:alkyl, cycloalkyl, alkenyl, cycloalkenyl, alkynyl, and aryl; wherein each of said substituent groups may be unsubstituted or substituted;{'sub': '3', 'sup': 2', '2', '2', '3, 'and each of said substituent groups optionally may contain one or more heteroatoms resulting in hetero-alkyl, hetero-cycloalkyl, hetero-alkenyl, hetero-cycloalkenyl, hetero-alkynyl, and hetero-aryl; and —CF, —CN, —C(O)OR, —C(O)R, and —C(O)NRR;'}{'sup': 2', '2', '2', '2', '2', '2', '3', '2', '3', '2', '2', '3', '2', '3', '2', '2', '3', '2, 'sub': 2', '2', '2', '2, 'said substituent group R bonded to X via an oxygen atom of said substituent group, is selected from the group consisting of —OR, —O(SO)R, —O(SO)R, —O(SO)OR, —O(SO)OR, —OS(O)NRR, —OS(O)NRR, —OPO(OR), —OPO(OR)OR, —OPO(R)OR, —OC(O)OR, —OC(O)NRR, and —OC(O)R;'}{'sub': 3', '2', '2, 'sup': 2', '2', '2', '2', '2', '2', '3', '2', '3, 'the substituent group R bonded to X via a sulphur atom of said substituent group, is selected from the group consisting of —SOR, —SR, —S(O)R, —S(O)R, —S(O)OR, —S(O)NRR, and —S(O)NRR; and'}{'sup': 2', '3', '2', '3', '2', '3', '4', '2', '3', '2', '3', '2', '3', '4', '2', '3', '2', '3', '2', '3', '4', '2', '3', '4', '2', '3', '2', '3 ...

Method for producing butadiene from ethanol with optimised in situ regeneration of the catalyst of the second reaction step

The present invention relates to a process for producing butadiene from ethanol, in two reaction steps, comprising a step a) of converting ethanol into acetaldehyde and a step b) of conversion into butadiene, said step b) simultaneously implementing a reaction step and a regeneration step in (n+n/2) fixed-bed reactors, n being equal to 4 or a multiple thereof, comprising a catalyst, said regeneration step comprising four successive regeneration phases, said step b) also implementing three regeneration loops.

METHODS, SYSTEMS, AND CATALYSTS FOR THE DIRECT CONVERSION OF SYNGAS TO HIGH-OCTANE HYDROCARBONS

The present disclosure relates to a method that includes converting a gas stream that contains hydrogen (H) and carbon monoxide (CO) to a second mixture that contains a hydrocarbon, for example, a hydrocarbon having between 3 and 15 carbon atoms, where the converting is performed using a first catalyst configured to convert Hand CO to methanol, a second catalyst configured to convert methanol to dimethyl ether (DME), and a third catalyst configured to convert DME to the hydrocarbon. 1. A method comprising:{'sub': '2', 'converting a gas stream comprising hydrogen (H) and carbon monoxide (CO) to a second mixture comprising a hydrocarbon having between 3 and 15 carbon atoms, wherein{'sub': '2', 'the converting is performed using a first catalyst configured to convert Hand CO to methanol,'}a second catalyst configured to convert methanol to dimethyl ether (DME), anda third catalyst configured to convert DME to the hydrocarbon.2. The method of claim 1 , wherein the first catalyst comprises copper and a zinc oxide.3. The method of claim 2 , wherein the first catalyst further comprises at least one of silica claim 2 , alumina claim 2 , zirconia claim 2 , or ceria.4. The method of claim 1 , wherein the second catalyst comprises at least one of an alumina or silica.5. The method of claim 1 , wherein the third catalyst comprises at least one of copper or a zeolite.6. The method of claim 5 , wherein the zeolite comprises a beta zeolite having a silica to alumina ratio between about 20:1 and about 300:1.7. The method of claim 6 , wherein the copper in the third catalyst is present at a concentration between about 1 wt % and about 20 wt % claim 6 , relative to the total weight of the third catalyst.8. The method of claim 1 , wherein the first catalyst and the second catalyst are present at a ratio between about 1:1 and about 8:1.9. The method of claim 8 , wherein the second catalyst and the third catalyst are present at a ratio between about 0.1:1 and about 5:2.10. The method of ...

FUNCTIONALIZED BORON NITRIDE CATALYSTS FOR THE PRODUCTION OF LIGHT OLEFINS FROM ALKANE FEEDS VIA OXIDATIVE DEHYDROGENATION

Disclosed is a catalyst comprising: a composition having a formula BNMOwherein B represents boron, N represents nitrogen, M comprises a metal or metalloid, and O represents oxygen, x ranges from 0 to 1, y ranges from 0.01 to 5.5; and z ranges from 0 to 16.5. The catalyst may be suitable for converting alkanes to olefins. 1. A catalyst comprising: {'br': None, 'sub': x', 'y', 'z, 'BNMO'}, 'a composition having a formula'} B represents boron, N represents nitrogen, M is platinum, silver, lanthanum, tin, cerium, zirconium, titanium, tin, strontium, magnesium, tungsten, copper, gallium, lithium, sodium, cesium, calcium, manganese, zinc, lead, barium, gallium, yttrium, ytterbium, silicon, cesium, germanium, niobium, vanadium, chromium, molybdenum, rhenium, or a combination thereof, and O represents oxygen,', 'x ranges from 0 to 1,', 'y ranges from 0.01 to 5.5; and', 'z ranges from 0 to 16.5., 'wherein'}2. The catalyst of claim 1 , wherein x ranges from 0.01 to 1.3. The catalyst of claim 1 , wherein x ranges from 0.9 to 1.4. The catalyst of claim 3 , wherein y and z range from 0.01 to 0.06.5. The catalyst of claim 4 , wherein y and z are 0.06.6. The catalyst of claim 5 , wherein x is equal to 1 and boron is present as a component of boron nitride.7. The catalyst of claim 3 , wherein y and z are equal.8. The catalyst of claim 3 , wherein M and O is speciated as magnesium oxide.9. The catalyst of claim 3 , wherein M is strontium and M and O is speciated as strontium oxide.10. The catalyst of claim 6 , wherein boron nitride is present as hexagonal boron nitride.11. The catalyst of claim 6 , wherein boron nitride is present as cubic claim 6 , wurtzitic claim 6 , or amorphous boron nitride.12. The catalyst of claim 3 , further comprising a support.13. The catalyst of claim 12 , wherein the catalyst is suitable for converting an alkane to an olefin and wherein the olefin comprises ethylene claim 12 , propylene claim 12 , butylene claim 12 , isobutene claim 12 , or a combination ...

SUPPORTED E/E' IRON CARBIDE CATALYST FOR FISCHER-TROPSCH SYNTHESIS REACTION, PREPARATION METHOD THEREOF AND FISCHER-TROPSCH SYNTHESIS PROCESS

The present disclosure relates to the technical field of Fischer-Tropsch synthesis reaction catalysts, and discloses a supported ε/ε′ iron carbide catalyst for Fischer-Tropsch synthesis reaction, preparation method thereof and Fischer-Tropsch synthesis process, wherein the method comprises the following steps: (1) dipping a catalyst carrier in a ferric salt aqueous solution, drying and roasting the dipped carrier to obtain a catalyst precursor; (2) subjecting the catalyst precursor and Hto a precursor reduction at the temperature of 300-550° C.; (3) pretreating the material obtained in the step (2) with Hand CO at the temperature of 90-185° C., wherein the molar ratio of H/CO is 1.2-2.8:1; (4) preparing carbide with the material obtained in the step (3), Hand CO at the temperature of 200-300° C., wherein the molar ratio of H/CO is 1.0-3.2:1. The preparation method has the advantages of simple and easily obtained raw materials, simple and convenient operation steps, being capable of preparing the catalyst with 100% pure phase ε/ε′ iron carbide as the active phase, the catalyst has lower selectivity of COand CHand higher selectivity of effective products. 110-. (canceled)11. A method of preparing a supported de iron carbide catalyst for Fischer-Tropsch synthesis reaction , wherein the preparation method comprises the following steps:(1) dipping a catalyst carrier in a ferric salt aqueous solution, drying and roasting the dipped carrier to obtain a catalyst precursor;{'sub': '2', '(2) subjecting the catalyst precursor and Hto a precursor reduction at the temperature of 300-550° C.;'}{'sub': 2', '2, '(3) pretreating the material obtained in the step (2) with Hand CO at the temperature of 90-185° C., wherein the molar ratio of H/CO is 1.2-2.8:1;'}{'sub': 2', '2, '(4) preparing carbide with the material obtained in the step (3), Hand CO at the temperature of 200-300° C., wherein the molar ratio of H/CO is 1.0-3.2:1.'}12. The method of claim 11 , wherein the ferric salt is ...

Catalysts, systems, and processes for regulating a contacting state in producing light olefins from paraffins

The present invention relates to catalysts, catalyst systems, and processes for the production of valuable light olefins, such as ethylene, from paraffinic hydrocarbons, such as propane, through dehydrogenation and metathesis. The contacting state between dehydrogenation and metathesis catalysts can advantageously be manipulated using an inert or relatively inert coating or outer shell that provides a degree of physical separation between catalytically active centers or inner cores. This has been discovered to significantly increase olefin selectivity (i.e., reduce undesired hydrogenation/hydrogenolysis side reactions) without an appreciable paraffin conversion deficit, such that the overall yield of desired olefinic hydrocarbons such as ethylene is thereby significantly increased.

METHOD FOR PRODUCING METHACRYLIC ACID ESTER

Production of methacrylic acid ester comprising a step of having acetone undergo a dehydration reaction in the presence of a dehydration reaction catalyst to obtain a reaction mixture; a step of separating a mixture containing propyne and propadiene as main components from the obtained reaction mixture; a step of separating the separated mixture containing propyne and propadiene as main components into a liquid, gas, or gas-liquid mixture containing propyne as a main component, and a liquid, gas, or gas-liquid mixture containing propadiene as a main component; and a step of bringing the obtained liquid, gas, or gas-liquid mixture containing propyne as a main component into contact with carbon monoxide and an alcohol having 1 to 3 carbon atoms in the presence of a catalyst containing at least one selected from the group consisting of Group 8 metal elements, Group 9 metal elements, and Group 10 metal elements. 1. A method for producing a methacrylic acid ester , which comprises the following steps:a dehydration reaction step: a step of having acetone undergo a dehydration reaction in the presence of a dehydration reaction catalyst to obtain a reaction mixture containing propyne, propadiene, and water;a propyne/propadiene separation step: a step of separating a mixture containing propyne and propadiene as main components from the reaction mixture obtained in the dehydration reaction step;a propyne purification step: a step of separating the mixture containing propyne and propadiene as main components separated in the propyne/propadiene separation step into a liquid, gas, or gas-liquid mixture containing propyne as a main component, and a liquid, gas, or gas-liquid mixture containing propadiene as a main component; anda carbonylation reaction step: a step of bringing the liquid, gas, or gas-liquid mixture containing propyne as a main component obtained in the propyne purification step into contact with carbon monoxide and an alcohol having 1 to 3 carbon atoms in the ...

AGGLOMERATED ODH CATALYST

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

Catalytic composition and process for the dehydrogenation of butenes or mixtures of butanes and butenes to give 1,3-butadiene

The present invention relates to a dehydrogenation process starting from reagents selected from single butenes, or mixtures thereof, or mixtures of butenes with butanes, to give 1-3 butadiene using catalytic composition of microspheroidal alumina and an active component containing a mixture comprising Gallium and/or Gallium oxides, Tin and/or Tin oxides, a quantity ranging from 1 ppm to 500 ppm with respect to the total weight of the catalytic composition of platinum and/or platinum oxides, and oxides of alkaline and/or alkaline earth metals.

Method of Forming a Catalyst with an Ion-Modified Binder

An alkylation catalyst having a zeolite catalyst component and a binder component providing mechanical support for the zeolite catalyst component is disclosed. The binder component is an ion-modified binder that can include metal ions selected from the group consisting of Co, Mn, Ti, Zr, V, Nb, K, Cs, Ga, B, P, Rb, Ag, Na, Cu, Mg, Fe, Mo, Ce, and combinations thereof The metal ions reduce the number of acid sites on the zeolite catalyst component. The metal ions can range from 0.1 to 50 wt % based on the total weight of the ion-modified binder. Optionally, the ion-modified binder is present in amounts ranging from 1 to 80 wt % based on the total weight of the catalyst.

SUPPORTED MULTIMETALLIC CATALYSTS FOR OXIDATIVE DEHYDROGENATION OF ALKANES

A catalyst for oxidative dehydrogenation of alkanes includes a substrate including an oxide; at least one promoter including a transition metal or a main group element of the periodic table; and an oxidation-active transition metal. The catalyst is multimetallic. 1. A catalyst for oxidative dehydrogenation of alkanes , the catalyst comprising:a substrate comprising an oxide;at least one promoter comprising a transition metal or a main group element of the periodic table; andan oxidation-active transition metal,wherein the catalyst is multimetallic.2. The catalyst of claim 1 , wherein the oxidation-active transition metal comprises manganese claim 1 , nickel or vanadium.3. The catalyst of claim 1 , wherein the oxidation-active transition metal comprises manganese.4. The catalyst of claim 1 , wherein the substrate is selected from the group consisting of SiO claim 1 , AlO claim 1 , TiO claim 1 , and ZrO.5. The catalyst of claim 1 , wherein the at least one promoter comprises a Lewis acidic and redox-active promoter.6. The catalyst of claim 1 , wherein the at least one promoter is selected from the group consisting of Cr claim 1 , Zr claim 1 , Ni claim 1 , and V.7. The catalyst of claim 1 , wherein the at least one promoter comprises an oxide layer of the transition metal or the main group element of the periodic table having a general formula of MO claim 1 , where M is the transition metal or the main group metal of the periodic table.8. The catalyst of claim 1 , wherein the at least one promoter is selected from the group consisting of Zn claim 1 , Fe claim 1 , Ga claim 1 , Cr claim 1 , Zr claim 1 , Ni claim 1 , and V.9. The catalyst of claim 1 , wherein the catalyst is doped with an element selected from the Group I elements of the periodic table claim 1 , the Group II elements of the periodic table claim 1 , or the main group elements of the periodic table.10. The catalyst of claim 1 , wherein the oxidation-active transition metal is dispersed on at least the ...

Methanation Catalyst

The invention relates to use of a catalyst comprising particles of nickel dispersed in a porous silica matrix for catalysing a methanation reaction. There is also described a method for methanation of a feedstock at least comprising gases carbon monoxide and hydrogen, said method comprising contacting the feedstock with the catalyst.

Hybrid Catalyst for Olefin Metathesis

An olefin metathesis catalyst and method for producing same is provided. 1. A method of preparing a hybrid metathesis catalyst , the method comprising the steps of:contacting a metathesis catalyst present in an organic solvent with a silica support containing a halogen or hydroxyl ligand capable of participating in a ligand exchange reaction;appending the metathesis catalyst to the silica support via the ligand exchange reaction to form a hybrid metathesis catalyst; andrecovering the hybrid metathesis catalyst from the organic solvent.2. The method of claim 1 , wherein the silica support is mesoporous silica.3. The method of claim 1 , wherein the metathesis catalyst contains a metal selected from the group consisting of tungsten claim 1 , molybdenum and ruthenium.4. The method of claim 1 , wherein the metathesis catalyst is benzylidene-bis(tricyclohexylphosphine)dichlororuthenium.5. The method of claim 1 , wherein the metathesis catalyst is benzylidene[1 claim 1 ,3-bis(2 claim 1 ,4 claim 1 ,6-trimethylphenyl)-2-imidazolidinylidene]dichloro(tricyclohexylphosphine)ruthenium.6. The method of claim 1 , wherein the organic solvent is toluene.7. The method of claim 1 , wherein the step of contacting the metathesis catalyst with the silica support is performed by an incipient wetness method.8. A method for the metathesis of butene to produce propene claim 1 , the method comprising the steps of: contacting a metathesis catalyst present in an organic solvent with a silica support containing a halogen or hydroxyl ligand capable of participating in a ligand exchange reaction;', 'appending the metathesis catalyst to the silica support via the ligand exchange reaction to form the hybrid metathesis catalyst; and', 'recovering the hybrid metathesis catalyst from the organic solvent;, 'providing, to a reaction chamber, a hybrid metathesis catalyst prepared bycontacting, in the reaction chamber, an olefin feedstream containing one or both of 1-butene or 2-butene with the hybrid ...

Diene production method

A method for producing diene comprises a step 1 of obtaining a straight chain internal olefin by removing a branched olefin from a raw material including at least the branched olefin and a straight chain olefin; and a step 2 of producing diene from the internal olefin by oxidative dehydrogenation using a first catalyst and a second catalyst, and the first catalyst has a complex oxide including bismuth, molybdenum and oxygen, and the second catalyst includes at least one selected from the group consisting of silica and alumina.

Aerosol processing method for controlled coating of surface species to generate catalysts

A method of producing a catalyst comprises generating an aerosolized flow of catalyst support particles, heating a catalytically active compound precursor to produce a catalytically active compound precursor vapor, contacting the aerosolized flow of catalyst support particles with the catalytically active compound precursor vapor, and condensing the catalytically active compound precursor onto the catalyst support particles to produce the catalyst comprising catalytically active compound deposited on surfaces of the catalyst support particles. The method may further comprise aerosolizing a catalyst support precursor mixture, drying the aerosolized catalyst support precursor mixture in a first heating zone to form an aerosolized flow of catalyst support particles, and contacting the catalyst support particles with a catalytically active compound precursor vapor in a second heating zone to form the catalyst comprising the layer of the catalytically active compound deposited on surfaces of the catalyst of catalyst support particles. 1. A method of producing a catalyst , the method comprising:generating an aerosolized flow of catalyst support particles;heating a catalytically active compound precursor to produce a catalytically active compound precursor vapor;contacting the aerosolized flow of catalyst support particles with the catalytically active compound precursor vapor; andcondensing the catalytically active compound precursor to produce the catalyst comprising a catalytically active compound deposited on surfaces of the catalyst support particles.2. The method of where the catalyst support particles comprise at least one of silica claim 1 , alumina claim 1 , or silica-alumina.3. The method of where the catalytically active compound precursor comprises at least one of tungsten claim 1 , platinum claim 1 , gold claim 1 , palladium claim 1 , rhodium claim 1 , iridium claim 1 , chromium claim 1 , rhenium claim 1 , molybdenum claim 1 , manganese claim 1 , titanium ...

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

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

Steam-Less Process for Converting Butenes to 1,3-Butadiene

Processes, systems, and catalysts for the conversion of 2-butene to 1,3-butaidene without the use of steam or, in some embodiments, with a reduced use of steam as compared to prior art processes are provided. The catalyst includes tungsten trioxide (WO) on an inorganic support includes activated magnesium oxide (MgO) and may be referred to as a “dual catalyst” or a “co-catalyst.” Embodiments of the catalyst. A process for the production of 1,3-butadiene may include contacting a feed stream of 2-butene with a WO-inorganic support catalyst or a MgO and WO-inorganic support catalyst and may be performed without steam in the feed stream. 1. A method for producing 1 ,3-butadiene , comprising:receiving a feed stream comprising 2-butene;contacting the feed stream with a catalyst in the presence of an oxidant to convert the 2-butene to 1-3-butadiene, the catalyst comprising tungsten oxide impregnated on an inorganic support.2. The method of claim 1 , wherein the feed stream does not include steam.3. The method of claim 1 , wherein the oxidant comprises air.4. The method of claim 1 , wherein the contacting is performed at a temperature in the range of 400° C. to 550° C.5. The method of claim 1 , wherein the feed stream comprises 1-butene.6. The method of claim 1 , wherein the inorganic support comprises silica.7. The method of claim 1 , wherein the catalyst comprises magnesium oxide.8. The method of claim 7 , wherein the magnesium oxide has a surface area in the range of 30 meters-squared/gram (m/g) to 200 m/g.9. The method of claim 7 , wherein the catalyst comprises a first layer of the tungsten oxide impregnated on the inorganic support claim 7 , a second layer of the tungsten oxide impregnated on the inorganic support claim 7 , and a layer of the magnesium oxide positioned between the first layer and the second layer.10. The method of claim 7 , wherein the catalyst comprises a layer of the magnesium oxide disposed on a layer of the tungsten oxide impregnated on the ...

OLEFIN CONVERSION PROCESS

Processes for the production of olefins are disclosed, which may include: contacting a hydrocarbon mixture comprising linear butenes with an isomerization catalyst to form an isomerization product comprising 2-butenes and 1-butenes; contacting the isomerization product with a first metathesis catalyst to form a first metathesis product comprising 2-pentene and propylene, as well as any unreacted Colefins, and byproducts ethylene and 3-hexene; and fractionating the first metathesis product to form a C3-fraction and a C5 fraction comprising 2-pentene. The 2-pentene may then be advantageously used to produce high purity 1-butene, 3-hexene, 1-hexene, propylene, or other desired products. 1. A system for the production of olefins , the system comprising: contacting a hydrocarbon mixture comprising linear butenes with an isomerization catalyst to form an isomerization product comprising 2-butenes and 1-butenes; and', {'sub': '4', 'contacting the isomerization product with a first metathesis catalyst to form a first metathesis product comprising 2-pentene and propylene, as well as any unreacted Colefins, and byproducts ethylene and 3-hexene;'}], 'an isomerization/metathesis reaction system fora fractionation system for fractionating the first metathesis product to form a C3-fraction and a C5 fraction comprising 2-pentene as essentially the only C5 olefin; anda flow conduit for feeding at least a portion of the C3-fraction to the isomerization/metathesis reaction system.2. The system of claim 1 , wherein the flow conduit for recycling the C3-fraction is configured to introduce the C3-fraction upstream of the isomerization catalyst claim 1 , upstream of the metathesis catalyst claim 1 , or both.3. The system of claim 1 , further comprising a metathesis reactor for contacting ethylene and the C5 fraction with a second metathesis catalyst claim 1 , which may be the same or different than the first metathesis catalyst claim 1 , to convert at least a portion of the 2-pentene and ...

SYSTEMS AND METHODS FOR PRODUCING PROPYLENE

According to one or more embodiments described herein, propylene may be produced by a process which may comprise one or more of at least partially metathesizing a first portion of a first stream to form a first metathesis-reaction product, at least partially cracking the first metathesis-reaction product to form a cracking-reaction product. 1. A process for producing propylene , the process comprising:at least partially metathesizing a first portion of a first stream to form a first metathesis-reaction product, the first stream comprising butene;at least partially cracking the first metathesis-reaction product to form a cracking-reaction product;combining a second stream with a second portion of the first stream to a form a mixed stream, the second stream comprising ethylene; andat least partially metathesizing the mixed stream to form a second metathesis-reaction product.2. The process of claim 1 , where the cracking reaction product comprises propylene and ethylene.3. The process of claim 1 , where the second metathesis-reaction product comprises propylene.4. The process of claim 1 , further comprising dividing the first stream into the first portion and the second portion.5. The process of claim 1 , where the first stream comprises at least 10 wt. % butene.6. The process of claim 1 , further comprising combining the cracking reaction stream with the second metathesis-reaction product to form a combined stream.7. The process of claim 6 , further comprising at least partially separating ethylene from the combined stream.8. The process of claim 6 , where the combined stream comprises at least 10 wt. % propylene.9. The process of claim 1 , where the cracking utilizes a mordenite framework inverted (MFI) structured silica catalyst10. The process of claim 1 , where the metathesis utilizes a mesoporous silica catalyst impregnated with metal oxide11. A process for producing propylene claim 1 , the process comprising:dividing a first stream into a first portion and a ...

Methods of Preparing an Aromatization Catalyst

Catalysts and method of preparing the catalysts are disclosed. One of the catalysts includes a zeolite support, a Group VIII metal on the zeolite support, and at least two halides bound to the zeolite support, to the Group VIII metal, or to both, and can have an average crush strength greater than 11.25 lb based on at least two samples of pellets of the catalyst measured in accordance with ASTM D4179. 1. A catalyst comprising: a zeolite support; a Group VIII metal on the zeolite support; and at least two halides bound to the zeolite support , to the Group VIII metal , or to both;wherein an average crush strength of the catalyst is greater than 11.25 lb based on at least two samples of pellets of the catalyst measured in accordance with ASTM D4179.2. The catalyst of claim 1 , wherein each of the at least two samples of pellets has 50 pellets.3. The catalyst of claim 1 , wherein the average crush strength is greater than 12 lb based on at least two samples of pellets of the catalyst measured in accordance with ASTM D4179.4. The catalyst of claim 1 , wherein an average crush strength per length of the catalyst is greater than about 2.48 lb/mm.5. The catalyst of claim 4 , wherein the average crush strength per length of the catalyst is in a range of from about 3.00 lb/mm to about 3.10 lb/mm.6. The catalyst of claim 1 , wherein less than 22% of the pellets that are measured in accordance with ASTM D4179 have an individual pellet crush strength of less than 10 lb/pellet.7. The catalyst of claim 6 , wherein less than 21% of the pellets that are measured in accordance with ASTM D4179 have an individual pellet crush strength of less than 10 lb/pellet.8. The catalyst of claim 1 , wherein less than 14% of the pellets that are measured in accordance with ASTM D4179 have an individual pellet crush strength of less than 9 lb/pellet.9. The catalyst of claim 8 , wherein less than 13% of the pellets that are measured in accordance with ASTM D4179 have an individual pellet crush ...

SYSTEM AND METHOD FOR HYDROGENATING AROMATIC COMPOUND

In a system for hydrogenation of an aromatic compound, an excessive temperature rise in the hydrogenation reaction unit is prevented, and the amount of the dilution gas to be circulated is minimized. The hydrogenation system () comprises a hydrogenation reaction unit () for producing a hydrogenated aromatic compound by adding hydrogen to an aromatic compound via a hydrogenation reaction, a separation unit () for separating the hydrogenated aromatic compound from a product of the hydrogenation reaction unit, and a transportation unit () for circulating at least a part of a residual component remaining in the separation unit after separating the hydrogenated aromatic compound therefrom to the hydrogenation reaction unit. The hydrogen supplied to the hydrogenation reaction unit consists of diluted hydrogen (L) diluted by a dilution compound having a higher molar specific heat than nitrogen, and the dilution compound includes a component circulated to the hydrogenation reaction unit as the residual component. 1. A system for hydrogenating an aromatic compound , comprising:a hydrogenation reaction unit for producing a hydrogenated aromatic compound by adding hydrogen to an aromatic compound via a hydrogenation reaction;a separation unit for separating the hydrogenated aromatic compound from a product of the hydrogenation reaction unit; anda transportation unit for circulating at least a part of a residual component remaining in the separation unit after separating the hydrogenated aromatic compound therefrom to the hydrogenation reaction unit;wherein the hydrogen supplied to the hydrogenation reaction unit consists of diluted hydrogen diluted by a dilution compound having a higher molar specific heat than nitrogen, and the dilution compound includes a component circulated to the hydrogenation reaction unit as the residual component.2. The system for hydrogenating an aromatic compound according to claim 1 , wherein the dilution compound in the diluted hydrogen is in a ...

SUPPORTED MULTIMETALLIC CATALYSTS FOR OXIDATIVE DEHYDROGENATION OF ALKANES

A catalyst for oxidative dehydrogenation of alkanes includes a substrate including an oxide; at least one promoter including a transition metal or a main group element of the periodic table; and an oxidation-active transition metal. The catalyst is multimetallic. 1. A catalyst for oxidative dehydrogenation of alkanes , the catalyst comprising:a substrate comprising an oxide;at least one promoter comprising a transition metal or a main group element of the periodic table; andan oxidation-active transition metal,wherein the catalyst is multimetallic.2. The catalyst of claim 1 , wherein the oxidation-active transition metal comprises manganese claim 1 , nickel or vanadium.3. The catalyst of claim 1 , wherein the substrate is selected from the group consisting of SiO claim 1 , AlO claim 1 , TiO claim 1 , and ZrO.4. The catalyst of claim 1 , wherein the at least one promoter comprises a Lewis acidic and redox-active promoter.5. The catalyst of claim 1 , wherein the at least one promoter comprises an oxide layer of the transition metal or the main group element of the periodic table having a general formula of MO claim 1 , where M is the transition metal or the main group metal of the periodic table.6. The catalyst of claim 1 , wherein the at least one promoter is selected from the group consisting of Zn claim 1 , Fe claim 1 , Ga claim 1 , Cr claim 1 , Zr claim 1 , Ni claim 1 , and V.7. The catalyst of claim 1 , wherein the catalyst is doped with an element selected from the Group I elements of the periodic table claim 1 , the Group II elements of the periodic table claim 1 , or the main group elements of the periodic table.8. A method of producing an alkene comprising:providing an alkane; and{'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'performing oxidative dehydrogenation on the alkane in the presence of an oxidant and the catalyst of to yield an alkene.'}9. The method of claim 8 , wherein the alkane and the oxidant are present in a 1:1 ratio.10. A method of ...

METHOD AND CATALYST FOR THE PRODUCTION OF 1,3-BUTADIENE FROM ETHANOL

The present invention is concerned with a catalyst for the conversion of ethanol to 1,3-butadiene comprising a component A selected from the list consisting of zeolite, silicon dioxide, aluminium oxide, or any combination thereof; and a component Bcomprising a mixed metal oxide, a catalyst precursor for the preparation of a catalyst for the conversion of ethanol to 1,3-butadiene comprising a component A selected from the list consisting of zeolite, silicon dioxide, aluminium oxide, or any combination thereof; and a component Bcomprising a layered double hydroxide (LDH) as well as a process for the conversion of ethanol to 1,3-butadiene, in which said catalyst is used. 1. A catalyst for the conversion of ethanol to 1 ,3-butadiene comprisingi) component A, which is selected from a list consisting of zeolite, silicon dioxide, aluminum oxide, or any combination thereof; and{'sub': 'cat', 'ii) component Bcomprising a mixed metal oxide.'}2. The catalyst according to claim 1 , wherein the weight ratio of component A to component Bis in the range from 1:0.05 to 1:2.5.3. The catalyst according to claim 1 , wherein the mixed metal oxide is a layered double oxide (LDO).4. The catalyst according to claim 1 , wherein the catalyst has a core-shell structure claim 1 , wherein the core of the core-shell structure comprises component A and the shell of the core-shell-structure comprises component B.5. A catalyst precursor for the preparation of a catalyst for the conversion of ethanol to 1 claim 1 ,3-butadiene comprisingi) component A, which is selected from a list consisting of zeolite, silicon dioxide, aluminum oxide, or any combination thereof; and{'sub': 'pre', 'ii) component Bcomprising a layered double hydroxide (LDH).'}6. The catalyst precursor according to claim 5 , wherein the weight ratio of component A to component Bis in the range from 1:0.1 to 1 :5.7. The catalyst precursor according to claim 5 , wherein the catalyst precursor has a core-shell structure claim 5 , ...

ALKANE ACTIVATION WITH SINGLE AND BI-METALLIC CATALYSTS

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

Multistage Nanoreactor Catalyst and Preparation and Application Thereof

The present disclosure discloses a multistage nanoreactor catalyst and preparation and application thereof, belonging to the technical field of synthesis gas conversion. The catalyst consists of a core of an iron-based Fischer-Tropsch catalyst, a transition layer of a porous oxide or porous carbon material, and a shell layer of a molecular sieve having an aromatization function. The molecular sieve of the shell layer can be further modified by a metal element or a non-metal element, and the outer surface of the molecular sieve is further modified by a silicon-oxygen compound to adjust the acidic site on the outer surface and the aperture of the molecular sieve, thereby inhibiting the formation of heavy aromatic hydrocarbons. According to the disclosure, the shell layer molecular sieve with a transition layer and a shell layer containing or not containing auxiliaries, and with or without surface modification can be prepared by the iron-based Fischer-Tropsch catalyst through multiple steps. The catalyst can be used for direct preparation of aromatic compounds, especially light aromatic compounds, from synthesis gas; the selectivity of light aromatic hydrocarbons in hydrocarbons can be 75% or above, and the content in the liquid phase product is not less than 95%; and the catalyst has good stability and good industrial application prospect. 1. A multistage nanoreactor catalyst , comprising a structure of a core , a shell body and a core-shell transition layer; wherein the core layer is an iron-based catalyst having Fischer-Tropsch activity , weight of the core layer being 0.1% to 80% of total weight of the catalyst; wherein the shell body is a molecular sieve , the weight of the shell body being 0.1% to 80% of the total weight of the catalyst; and wherein the core-shell transition layer is a porous oxide or porous carbon material , the weight of the transition layer being 0.01% to 35% of the total weight of the catalyst.2. The multistage nanoreactor catalyst according ...

HIGH TEMPERATURE CCR PROCESS WITH INTEGRATED REACTOR BYPASSES

A process is presented for increasing the aromatics content in a reformate process stream. The process modifies existing processes to change the operation without changing the reactors or heating units. The process includes bypasses to utilize heating capacity of upstream heating units, and passes the excess capacity of the upstream heating units to downstream process streams. 1. A process for increasing the aromatic content of a hydrocarbon stream , comprising:passing the hydrocarbon stream through a series of reforming reactors and reactor feed heaters, wherein the reactors feed heaters generate a heated stream and at least one of the heated streams is split into a first portion and a second portion, with the first portion passed to a reforming reactor to generate a reforming reactor effluent stream; andwherein the second portion of the heated stream is combined with a downstream reforming reactor effluent stream and the combined stream is passed to a downstream reactor feed heater, to generate a reactor product stream with increased aromatic content.2. The process of wherein the first reactor is operated at a first temperature claim 1 , and the subsequent reactors are operated at a second temperature and the second temperature is greater than the first temperature.3. The process of further comprising:splitting at least one reactor effluent stream into a first portion and a second portion;passing the first portion of the effluent stream with the second portion of the heated stream to a reactor interheater; andcombining the second portion of the effluent stream with a downstream heated feedstream to a downstream reactor.4. The process of wherein the downstream reactor is the next reactor in the series of reactors.5. The process of wherein the downstream reactor is the reactor after the next reactor in the series of reactors.6. The process of wherein the first reaction temperature is between 400° C. and 500° C.7. The process of wherein there are at least two ...

SELECTIVE ALKANE ACTIVATION WITH SINGLE-SITE ATOMS ON AMORPHOUS SUPPORT

The present invention relates generally to catalysts and methods for use in olefin production. More particularly, the present invention relates to novel amorphously supported single-center, Lewis acid metal ions and use of the same as catalysts. 1. A catalyst for use in olefin production comprising one or more single-atom Lewis acid metal ions on the surface of an amorphous support , wherein said catalyst selectively cleaves C—H bonds over C—C bonds in the conversion of alkenes to alkanes.2. The catalyst of claim 1 , wherein the Lewis acid metal is selected from the group consisting of Fe claim 1 , Co claim 1 , Zn claim 1 , Ni claim 1 , Ti claim 1 , Sc claim 1 , Zr claim 1 , Hf claim 1 , Ce claim 1 , Ta claim 1 , La claim 1 , Ga claim 1 , and the lanthanides.3. The catalyst of claim 2 , wherein the Lewis acid metal is selected from the group consisting of Fe claim 2 , Co claim 2 , Zn claim 2 , and Ga.4. The catalyst of claim 2 , wherein the amorphous support is a refractory oxide.5. The catalyst of claim 4 , wherein the refractory oxide is selected from the group consisting of TiO claim 4 , ZrO claim 4 , CeO claim 4 , AlzO claim 4 , MgO claim 4 , and mixtures of these.6. The catalyst of claim 5 , wherein the amorphous support is a silica support.7. The catalyst of claim 4 , wherein the lewis acid metal ion is tetrahedrally coordinated.8. The catalyst of claim 7 , wherein the catalyst is a heterogeneous claim 7 , single-site Zn(II) catalyst claim 7 , in which the tetrahedrally coordinated Zn(II) ion is bonded to the silica support at 3-membered ring siloxane sites.9. The catalyst of claim 1 , wherein the catalyst is not redox-active.10. The catalyst of claim 1 , wherein the catalyst has a selectivity of greater than 75% for C—H activation.11. The catalyst of claim 1 , wherein the catalyst has a selectivity of greater than 90% for C—H activation.12. The catalyst of claim 1 , wherein the catalyst has a selectivity of greater than 95% for C—H activation.13. The catalyst ...

USE OF CATALYST PREPARED WITH A SUBGROUP VI ELEMENT FOR THE PRODUCTION OF ORGANIC CHEMICALS AND FUELS FROM LIGNIN

A subgroup VI element to prepare a catalyst for the production of organic chemicals and fuels from lignin with the involvement of solvent molecules. The catalytic reaction use a catalyst composed of a molybdenum or tungsten compound as the active phase, with mixing a kind of lignin, a catalyst, and a reactive solvent. An inert or reductive gas such as H2, N2 or Ar is used to purge or fill the reaction vessel. The temperature is above 200° C., the reaction time is sufficient. The liquid product is separated and analyzed; a catalytic process with a very high product yield, up to 90% if calculated accounting the parts from lignin of the product molecules, or up to over 100% if calculated as the mass products. The product includes aromatic compounds, esters, alcohols, monophenols and benzyl alcohols in different ratios according to the composition, the solvent and the other reaction conditions. 1. The characterization of the application of a catalyst prepared with a subgroup VI element for the production of organic chemicals and fuels from lignin is that the lignin , catalyst and solvent were mixed in the sealed reactor. Reductant or inert gas was used to purge the reactor and then the temperature was increased above 200° C. Finally , liquid products were obtained after sufficient reaction time. The solvents employed were deionized water , ethanol or a mixture of water and ethanol with any proportion.2. The characterization of the application of a catalyst prepared with a subgroup VI element for the production of organic chemicals and fuels from lignin in is that the lignin employed includes Kraft lignin claim 1 , alkali lignin claim 1 , Klason lignin claim 1 , enzymatic hydrolysis lignin claim 1 , milled wood lignin and organosolv lignin. The inert gas is nitrogen claim 1 , argon or helium and the reductive gas is hydrogen. The volume fraction of ethanol is 0-100% in the mixture of water and ethanol with any proportion. The liquid products are alcohols claim 1 , esters ...

FISCHER-TROPSCH PROCESS IN THE PRESENCE OF A CATALYST PREPARED FROM A MOLTEN SALT

Fischer-Tropsch process for the synthesis of hydrocarbons by bringing a feedstock including synthesis gas into contact with a catalyst prepared by the following: 1. Fischer-Tropsch process for the synthesis of hydrocarbons , which comprises bringing a feedstock comprising a synthesis gas into contact with at least one catalyst under a total pressure between 0.1 and 15 MPa , at a temperature of between 150 and 350° C. , and at an hour space velocity of between 100 and 20 000 volumes of synthesis gas per volume of catalyst and per hour with an H/CO molar ratio of the synthesis gas between 0.5 and 4 , said catalyst containing an active phase comprising at least cobalt and a porous support of oxide type , said catalyst being prepared by at least the following steps:a) said porous oxide-type support is brought into contact with a cobalt metal salt of which the melting point of said cobalt metal salt is between 30 and 150° C., in order to form a solid mixture for a period of time of between 5 minutes and 5 hours, the weight ratio of said cobalt metal salt to said porous oxide support being between 0.1 and 1;b) the solid mixture obtained at the end of step a) is heated with stirring under atmospheric pressure at a temperature between the melting point of said cobalt metal salt and 200° C. for a period of time of between 5 minutes and 12 hours;c) optionally, the solid obtained at the end of step b) is dried at a temperature below 200° C.;d) the solid obtained at the end of step b) or c) is calcined at a temperature above 200° C. and below or equal to 1100° C. under an inert atmosphere or under an oxygen-containing atmosphere.2. Process according to claim 1 , in which said cobalt metal salt is chosen from cobalt nitrate hexahydrate or cobalt acetate tetrahydrate.3. Process according to claim 1 , in which the weight ratio of the cobalt metal salt to the porous support is between 0.3 and 0.9.4. Process according to claim 1 , in which step a) is carried out for 10 minutes to 4 ...

Production and Use of 3,4' and 4,4'-Dimethylbiphenyl Isomers

In a process for producing 3,4′ and/or 4,4′ dimethyl-substituted biphenyl compounds, a feed comprising toluene is contacted with hydrogen in the presence of a hydroalkylation catalyst under conditions effective to produce a hydroalkylation reaction product comprising (methylcyclohexyl)toluenes. At least part of the hydroalkylation reaction product is dehydrogenated in the presence of a dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising a mixture of dimethyl-substituted biphenyl isomers. The dehydrogenation reaction product is then separated into at least a first stream containing at least 50% of 3,4′ and 4,4′ dimethylbiphenyl isomers by weight of the first stream and at least one second stream comprising one or more 2,x′ (where x′ is 2′, 3′, or 4′) and 3,3′ dimethylbiphenyl isomers. 1. A process for producing 3 ,4′ and/or 4 ,4′ dimethyl-substituted biphenyl compounds , the process comprising:(a2) contacting a feed comprising benzene with hydrogen in the presence of a hydroalkylation catalyst under conditions effective to produce a hydroalkylation reaction product comprising cyclohexylbenzenes;(b2) dehydrogenating at least part of the hydroalkylation reaction product in the presence of a dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising biphenyl;(c2) reacting at least part of the dehydrogenation reaction product with a methylating agent in the presence of an alkylation catalyst under conditions effective to produce a methylation reaction product comprising a mixture of dimethyl-substituted biphenyl isomers; and(d2) separating the methylation reaction product into at least a first stream containing at least 50% of 3,4′ and 4,4′ dimethylbiphenyl isomers by weight of the first stream and at least one second stream comprising one or more 2,X′ (where X′ is 2′, 3′, or 4′) and 3,3′ dimethylbiphenyl isomers.2. The process of claim 1 , wherein the ...

Catalyst for oxygen-free direct conversion of methane and method of converting methane using the same

The present invention relates to a catalyst for oxygen-free direct conversion of methane and a method of converting methane using the same, and more particularly to a catalyst for oxygen-free direct conversion of methane, in which the properties of the catalyst are optimized by adjusting the free space between catalyst particles packed in a reactor, thereby maximizing the catalytic reaction rate without precise control of reaction conditions for oxygen-free direct conversion of methane, minimizing coke formation and exhibiting stable catalytic performance even upon long-term operation, and to a method of converting methane using the same.

METHOD FOR ISOMERISING DEHYDRATION OF A NON-LINEAR PRIMARY MONOALCOHOL ON A QUADRILOBED IRON ZEOLITE CATALYST

A method for isomeris ng dehydration in the presence of a specific catalyst, to produce at least one alkene, carried out on a feedstock containing a non-linear primary monoalcohol, where the catalyst includes a zeolite having a series of 8MR channels and a binder having certain pore volume, which catalyst is multilobe-shaped and has characteristics including certain average mesopore volume Vm, and mesopores having a certain diameter, an average certain macropore volume VM, the macropores having a certain diameter, and certain average micropore volume Vμ, the micropores having a certain diameter, and the catalyst has a certain exposed geometric area. 1. A process for isomerizing dehydration of a feedstock comprising , alone or in a mixture , a primary monoalcohol of formula R—CH—OH , in which R is a nonlinear alkyl radical of general formula CHwhere n is an integer of between 3 and 20 , said process comprising a step of isomerizing dehydration operated in the gas phase at a weighted average temperature of between 250 and 460° C. , at a pressure of between 0.2 MPa and 1 MPa , at a weight hourly space velocity (WWH) of between 1 and 25 h , in the presence of a catalyst comprising at least one zeolite and at least one binder , in which the amount by weight Tz of zeolite is 55-90 wt % relative to the total weight of said catalyst and in which said zeolite has at least one series of channels with an aperture of 8 oxygen atoms (8MR) , said binder having a pore volume of between 0.5 and 0.9 ml/g , the catalyst being multilobate and havingan average mesopore volume Vm centered at plus or minus 20% around the value defined by the formula Vm=−0.004Tz+0.505, the mesopores having a diameter of 3.6 nm to 50 nm,an average macropore volume VM centered at plus or minus 20% around the value defined by the formula VM=0.0101Tz 0.5375, the macropores having a diameter of more than 50 nm and less than 7000 nm,an average micropore volume Vμ centered at plus or minus 20% around the value ...

Chromium-Based Catalysts and Processes for Converting Alkanes into Higher and Lower Aliphatic Hydrocarbons

Processes for cracking an alkane reactant to form a lower aliphatic hydrocarbon product and for converting an alkane reactant into a higher aliphatic hydrocarbon product are disclosed, and these processes include a step of contacting the alkane reactant with a supported chromium (II) catalyst. In addition to the formation of various aliphatic hydrocarbons, such as linear alkanes, branched alkanes, 1-alkenes, and internal alkenes, aromatic hydrocarbons and hydrogen also can be produced.

Processes for conversion of biologically derived mevalonic acid

A process is provided for converting mevalonic acid into various useful products and derivatives. More particularly, the process comprises reacting mevalonic acid, or a solution comprising mevalonic acid, in the presence of a solid catalyst at an elevated temperature and pressure to thereby form various biobased products. The process may also comprise: (a) providing a microbial organism that expresses a biosynthetic mevalonic acid pathway; (b) growing the microbial organism in fermentation medium comprising suitable carbon substrates, whereby biobased mevalonic acid is produced; and (c) reacting the biobased mevalonic acid in the presence of a solid catalyst at an elevated temperature and pressure to yield various biobased products.

PROCESS FOR THE PRODUCTION OF 1,3-BUTADIENE

The invention relates to the use of a novel silica-supported trimetallic (La/Zr/Zn) catalyst in the production of 1,3-butadiene from ethanol. The presence of lanthanum in the catalyst further comprising zirconium and zinc increases the catalyst's yield and selectivity to 1,3-butadiene. 1. A process for the production of 1 ,3-butadiene , the process comprisingi) providing a supported catalyst comprising lanthanum, zirconium, and zinc, the support comprising silica; andii) contacting a feed comprising ethanol with the supported catalyst, to obtain a raw product comprising 1,3-butadiene.2. The process according to claim 1 , wherein contacting ii) takes place at a temperature in a range of 300 to 425° C.3. The process according to claim 1 , wherein contacting ii) takes place at a weight hourly space velocity of 0.2-7 h.4. The process according to claim 1 , wherein the feed additionally comprises acetaldehyde.5. The process according to claim 1 , wherein it further comprisesiii) separating the raw product into a first portion comprising 1,3-butadiene and a second portion comprising acetaldehyde.6. The process according to claim 5 , wherein at least part of the second portion is recycled into the feed.8. The process according to claim 7 , wherein the method further comprisesd) impregnating the calcined dried impregnated support of step c) with a salt of zirconium and a salt of zinc;e) drying the impregnated support of step d); andf) calcining the dried impregnated support of step e).9. The process according to claim 7 , wherein claim 7 , in said method claim 7 , the support is impregnated in step a) with a salt of lanthanum claim 7 , a salt of zirconium claim 7 , and a salt of zinc.10. Use of lanthanum in a catalyst for the production of 1 claim 7 ,3-butadiene from a feed comprising ethanol and optionally acetaldehyde claim 7 , to increase the selectivity of the catalytic reaction to 1 claim 7 ,3-butadiene claim 7 , the catalyst further comprising zirconium and zinc. The ...

INTEGRATED C3 - C4 HYDROCARBON DEHYDROGENATION PROCESS

An integrated process, suitable for use in a new or retrofitted plant, produces an olefin or di-olefin via the dehydrogenation of an appropriate C3-C4 hydrocarbon feed includes (1) contacting the feed and a dehydrogenation catalyst having a Geldart A or Geldart B classification in a fluidized bed at a temperature from 550° C. to 760° C. and a pressure from about 41.4 to about 308.2 kPa (about 6.0 to about 44.7 psia) and a catalyst to feed ratio, w/w, from 5 to 100 to form a dehydrogenate product; separating the dehydrogenate product and unreacted starting feed mixture from a portion of the catalyst by means of a cyclonic separation system; reactivating the catalyst in a fluidized regenerator by combustion at 660° C. to 850° C., followed by contact with an oxygen-containing fluid at 660° C. or greater, and returning the catalyst to the dehydrogenation reactor; (2) compressing the product mixture to form a compressed product mixture; and (3) fractionating the compressed product mixture to form a product stream including at least the target olefin or di-olefin. The integrated process offers increased plant capacity, improved economics, and reduced environmental impact in comparison with other known and conventional processes. 1. An integrated process for producing C3-C4 olefins or C3-C4 di-olefins comprising the steps of: (i) a C3-C4 hydrocarbon feed and', '(ii) a catalyst feed comprising a catalyst meeting the requirements of a Geldart A or Geldart B classification;, '(1) (a) contacting, in a fluidized dehydrogenation reactor,'}at a ratio of catalyst feed to C3-C4 hydrocarbon feed of from 5 to 100 on a weight to weight basis;wherein optionally the C3-C4 hydrocarbon feed and the catalyst feed have been preheated to a temperature of from about 400° C. to about 660° C.; andwherein the average contact time between the C3-C4 hydrocarbon feed and the catalyst feed is from about 1 second to about 10 seconds; andwherein the reaction temperature in the fluidized ...

Multimetallic mixed oxides, its preparation and use for the oxidative dehydrogenation of ethane for producing ethylene

A layered multimetallic oxide catalyst having the formula M1 M2 M3 O δ wherein: M1 is selected from the group of Ag, Au, Zn, Sn, Rh, Pd, Pt, Cu, Ni, Fe, Co, an alkaline metal, an alkaline earth metal, a rare earth metal, and mixtures thereof; M2 is selected from the group of Ti, Hf, Zr, Sn, Bi, Sb, V, Nb, Ta and P, and mixtures thereof; M3 is selected from the group of Mo, W and Cr, and mixtures thereof; and where said multilayered metallic oxide exhibits a major X-ray diffraction peak between 5<2θ<15, is prepared by a process of mixing metallic precursors of M 1 , M 2 and M 3 to form a precursor mixture, hydrothermal treatment of the resulting mixture to obtain a homogeneous solid mixture, and thermally treating the solid mixture to activate the solid mixture and obtain said catalyst.

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 ...

Method and Reactor for Oxidative Coupling of Methane

A method of autothermal oxidative coupling of methane (OCM) utilizes introducing a methane-containing feedstock and an oxygen-gas-containing feedstock into a reactor () as a flowing mixture () with a space time of 500 ms or less. The reactor () contains a catalyst bed () of an OCM catalyst that contacts the flowing mixture and wherein the catalyst bed () has a heat Peclet number (Pe) of from 5 or less, a mass Peclet number (Pe) of from 5 or more, and a transverse Peclet number (P) of from 1 or less while contacting the flowing mixture. The methane and oxygen of the feedstocks are allowed to react within the reactor () to form methane oxidative coupling reaction products. A reactor () for carrying out the OCM reaction is also disclosed. 1. A method of carrying out autothermal oxidative coupling of methane (OCM) comprising:{'sub': h', 'm, 'introducing a methane-containing feedstock and an oxygen-gas-containing feedstock into a reactor as a flowing mixture with a space time of 500 ms or less, the reactor containing a catalyst bed of an OCM catalyst that contacts the flowing mixture and wherein the catalyst bed has a heat Peclet number (Pe) of from 5 or less, a mass Peclet number (Pe) of from 5 or more, and a transverse Peclet number (P) of from 1 or less while contacting the flowing mixture; and'}allowing the methane and oxygen of the feedstocks to react within the reactor to form methane oxidative coupling reaction products.2. The method of claim 1 , wherein: a layer of OCM catalyst formed as catalyst particles having a particle size of from 0.1 mm to 3 mm;', 'at least one monolithic body of one of a ceramic or metal material having pores or channels with a pore or channel size from 0.1 to 5 mm, the monolithic body having an OCM catalyst material present on at least all or a portion of the surface of the monolithic body;', 'at least one monolithic body of one of a ceramic or metal material having pores or channels with a pore or channel size from 0.1 to 5 mm, and ...

CATALYTIC ETHENOLYSIS OF OPTIONALLY-FUNCTIONALIZED INTERNAL UNSATURATED OLEFINS

The disclosure relates to a process for obtaining alpha-olefins by heterogeneous catalytic ethenolysis of optionally-functionalized unsaturated, in particular mono-unsaturated, olefins. The disclosure also relates to new supported catalysts that can be used in the process and to a method for preparing the supported catalysts. 1. A process for obtaining alpha-olefins , said process comprising a step of reacting optionally-functionalized internal unsaturated olefins with ethylene in the presence of a supported catalyst selected from a supported oxo-molybdenum or imido-molybdenum catalyst or a supported oxo-tungsten catalyst , [{'br': None, 'sub': 2', '2, 'sup': 1', '2, '□-W(═O)X(CHR)(CHR)\u2003\u2003(I)'}, {'br': None, 'sub': 2', '2', '2, 'sup': 1', '2, '(□)W(═O)(CHR)(CHR)\u2003\u2003(III)'}], 'said oxo-tungsten catalyst being selected from one of the following oxo-tungsten compounds {'br': None, 'sup': k', '4', '5, '□-OLO—Mo(═NR)G(═CHR)\u2003\u2003(VIII)'}, 'said imido-molybdenum catalyst being selected from one of the following imido-molybdenum compoundswherein,□ corresponds to a support,{'sup': 1', '2', '1', '2, 'sub': 3', '3', '3', '3', '3', '2, 'Rand R, are independently to each other, selected from hydrogen, linear or branched alkyl groups, —C(CH), -Phenyl, —Si(CH), —C(CH)Ph, being understood that Rand Rcannot be both hydrogen in formula (III),'}{'sub': 3', '3, 'X is selected from alkoxy groups, aryloxy groups, —Si(CH), siloxy groups or pyrolidyl groups,'}{'sup': '4', 'Rrepresents a radical selected from aliphatic and aromatic hydrocarbyl radicals, optionally comprising one or more heteroatoms,'}{'sup': '5', 'sub': 3', '3', '3', '3', '3', '2, 'Ris selected from hydrogen, linear or branched alkyl groups, —C(CH), -Phenyl (Ph), —Si(CH), or —C(CH)Ph,'}G is selected from alkoxy groups, aryloxy groups, siloxy groups or pyrolidyl groups,{'sup': 'k', 'Lrepresents a divalent linker.'}2. The process according to claim 1 , wherein the optionally-functionalized internal ...

Methods of Preparing an Aromatization Catalyst

Catalysts and method of preparing the catalysts are disclosed. One of the catalysts includes a zeolite support, a Group VIII metal on the zeolite support, and at least two halides bound to the zeolite support, to the Group VIII metal, or to both, and can have an average crush strength greater than 11.25 lb based on at least two samples of pellets of the catalyst measured in accordance with ASTM D4179.

CATALYST COMPOSITION FOR ENHANCING YIELD OF OLEFINS IN FLUID CATALYTIC CRACKING PROCESS (FCC)

The present invention provides a catalyst composition comprising rare earth exchanged USY zeolite (REUSY); pentasil zeolite; phosphorous compound; clay, silica, alumina, and spinel to enhance the catalytic activity and selectivity for light olefins in FCC operation conditions. The present invention also provides a process for the preparation of Light olefin enhancing catalyst composition with high propylene yield and coke selectivity. 1. A composite catalyst composition , comprising:about 10-25 wt % rare earth exchanged USY zeolite (REUSY);about 5-20 wt % stabilized pentasil zeolite;about 2-8 wt % phosphorous compound;about 20-45 wt % clay;about 5-25 wt % silica;about 10-35 wt % alumina; andabout 0.5 to 3 wt % mixed metal oxide selected from a group consisting of at least one of Group XI and XIII metals, and the wt % being based on total weight of the catalyst composition.2. The composition as claimed in claim 1 , wherein the mixed metal oxide is a spinel.3. The composition as claimed in claim 1 , wherein the mixed metal oxide comprises of oxides of metals selected from at least one of copper claim 1 , nickel claim 1 , zinc claim 1 , aluminium claim 1 , and mixtures thereof.4. The composition as claimed in claim 1 , wherein the pentasil zeolite is selected from a group consisting of ZSM-5 claim 1 , ZSM-11 claim 1 , mordenite claim 1 , and beta.5. The composition as claimed in claim 1 , wherein the REUSY comprises of 0.1 to 5 wt % of rare earth oxide.6. The composition as claimed in claim 1 , wherein the phosphorous compound is sourced from a group consisting of at least one of mono-ammonium phosphate claim 1 , di-ammonium phosphate claim 1 , and phosphoric acid.7. The composition as claimed in claim 1 , wherein the clay is selected from a group consisting of at least one of bentonite claim 1 , attapulgite claim 1 , and kaolinite.8. The composition as claimed in claim 1 , wherein the silica is selected from at least one of sodium and ammonium stabilized colloidal ...

PROCESS TO PREPARE PROPYLENE

The invention is directed to a process to prepare propylene from a hydrocarbon feed comprising pentane by contacting the hydrocarbon feed with a heterogeneous cracking catalyst as present in one or more fixed beds thereby obtaining a cracked effluent. The heterogeneous catalyst comprises a matrix component and a molecular sieve comprising framework alumina, framework silica and a framework metal selected from the group of Zn, Fe, Ce, La, Y, Ga and/or Zr. Propylene is isolated from the cracked effluent. 1. A process to prepare propylene from a hydrocarbon feed comprising pentane by contacting the hydrocarbon feed with a heterogeneous cracking catalyst as present in one or more fixed beds thereby obtaining a cracked effluent ,wherein the heterogeneous catalyst comprises a matrix component and a molecular sieve comprising framework alumina, framework silica and a framework metal selected from the group of Zn, Fe, Ce, La, Y, Ga and/or Zr andwherein propylene is isolated from the cracked effluent.2. The process according to claim 1 , wherein the framework metal is selected from the group of Fe or Ga3. The process according to claim 2 , wherein the framework metal is Fe.4. The process according to claim 1 , wherein the atomic ratio between framework Al and framework metal is between 1:0.05 and 1:0.55. A process to prepare propylene from a hydrocarbon feed comprising pentane by contacting the hydrocarbon feed with a heterogeneous cracking catalyst as present in one or more fixed beds thereby obtaining a cracked effluent claim 1 ,{'sub': '3', 'wherein the heterogeneous catalyst comprises a matrix component and a modified molecular sieve comprising framework alumina and framework silica and wherein the catalyst is obtainable by (i) crystallization of a synthesis gel comprising FeClthereby obtaining a molecular sieve product comprising of framework Al, Si and Fe, (ii) calcining, (iii) mixing with the matrix and (iv) calcined until the molecular sieve had a framework Fe to ...

MULTIMETALLIC CATALYSTS

A multimetallic catalyst having a substrate, promoter and catalytic metal. 1. A catalyst for n-butane dehydrogenation comprising:a substrate surface consisting essentially of an oxide;{'sub': 'x', 'a promoter consisting essentially of MOwhere M is a transition metal or main group elemental oxide, the promoter deposited on the substrate;'}a catalytic metal consisting essentially of a platinum group metal promoter.2. The catalyst of claim 1 , wherein the catalyst exhibits at least 10-60% selectivity for 1 claim 1 ,3 butadiene.3. The catalyst of claim 1 , wherein the catalyst exhibits 40-99% 1 claim 1 ,3-butadiene conversion.4. The catalyst of claim 1 , further comprising a dopant.5. The catalyst of claim 4 , wherein the dopant is boron.6. The catalyst of claim 1 , wherein the dopant is selected from the group consisting of a group 13 element claim 1 , group 1 cation and group 2 cation.7. The catalyst of claim 1 , wherein the substrate comprises an oxide of a material selected from the group consisting of Si claim 1 , Al claim 1 , Ti claim 1 , and Zn.8. The catalyst of claim 7 , wherein M is a transition metal.9. A method of forming 1 claim 7 ,3 butadiene comprising:{'sub': x', 'y, 'exposing n-butane to a catalyst comprising M′/M/EOwhere the catalyst M′ is a Pt group metal, M is a transition metal or a main group element material and E is Si, Al, Ti, or Zr and x and y represent stoichiometric amounts; forming 1,3 butadiene.'}10. The method of wherein forming the 1 claim 9 ,3 butadiene comprises a selectivity for 1 claim 9 ,3 butadiene of 10-60%.11. The method of claim 9 , wherein exposing the n-butane is at a temperature of between 250° C. and 650° C.12. The method of claim 11 , where the temperature is 500° C. to 600° C.13. The method of claim 9 , wherein exposing the n-butane comprises exposing the n-butane to at least 3.6 mg of catalyst.14. The method of claim 13 , wherein exposing the n-butane comprises exposing the n-butane to at least 13 mg of catalyst.15. The ...

CONVERSION OF PROPANE TO PROPYLENE

A process is disclosed that includes brominating a C, C, C, Cor Calkane with elemental bromine to form a bromo-alkane. The bromo-alkane is reacted to form a C, C, C, Cor Calkene and HBr. The HBr is oxidized to form elemental bromine. 1. A process comprising:{'sub': 2', '3', '4', '5', '6, 'brominating an alkane with elemental bromine to form a bromo-alkane and dibromo-alkane, wherein the alkane is a C, C, C, Cor Calkane;'}reacting the bromo-alkane to form a corresponding alkene of the alkane and HBr; andoxidizing the HBr to form elemental bromine.2. The process of claim 1 , wherein the alkane is ethane claim 1 , propane claim 1 , n-butane claim 1 , isobutane claim 1 , a pentane claim 1 , or a hexane.3. The process of claim 2 , wherein the alkane is propane and the alkene is propylene.4. A process comprising:providing a feedstock comprising propane;reacting at least some of the propane with bromine to form bromopropane, dibromopropane, and HBr;dehydrobrominating the bromopropane to form a propylene and HBr mixture;separating the propylene and HBr mixture to form propylene and recycle HBr;oxidizing the recycle HBr to form a bromine and water mixture; andseparating bromine from the bromine and water mixture.5. The process of claim 4 , wherein the step of reacting at least some of the propane with bromine is thermally induced.6. The process of claim 5 , wherein the reaction occurs at a temperature of at least 200° C.7. The process of claim 4 , wherein the dehydrobrominating step takes place in the presence of a catalyst.8. The process of claim 7 , wherein the catalyst is selected from the group consisting of a silica-based catalyst claim 7 , titanium dioxide claim 7 , zirconium dioxide and their mixtures thereof9. The process of claim 7 , wherein in the dehydrobrominating step claim 7 , the bromopropane is heated to between 250° C. and 500° C.10. The process of claim 4 , wherein separating the propylene and HBr mixture is accomplished by distillation.11. The process of ...

CATALYSTS FOR PETROCHEMICAL CATALYSIS

Metal oxide catalysts comprising various dopants are provided. The catalysts are useful as heterogenous catalysts in a variety of catalytic reactions, for example, the oxidative coupling of methane to C2 hydrocarbons such as ethane and ethylene. Related methods for use and manufacture of the same are also disclosed. 185-. (canceled)87. The catalyst of claim 86 , wherein A is from groups 2 claim 86 , 3 or 4.88. The catalyst of claim 86 , wherein A is Ce claim 86 , Pr claim 86 , Sr claim 86 , Ca claim 86 , Mg claim 86 , Y claim 86 , Zr or Ba.89. The catalyst of claim 86 , wherein B is from group 4.90. The catalyst of claim 86 , wherein B is Zr or Hf.91. The catalyst of claim 86 , wherein the dopant is Sr claim 86 , Mg or Ca.92. The catalyst of claim 86 , wherein the catalyst comprises one of the following formulas: Y/SrZrO claim 86 , SrHfO claim 86 , SrZrO claim 86 , Mg/SrHfO claim 86 , CaHfOor SrTbO.93. The catalyst of claim 86 , wherein the catalyst is a bulk catalyst.94. The catalyst of claim 86 , wherein the catalyst is a nanostructured catalyst.95. The catalyst of claim 94 , wherein the catalyst is a nanowire.96. A method for the oxidative coupling of methane claim 86 , the method comprising contacting methane with the catalyst of at temperatures ranging from about 550° C. to about 750° C. claim 86 , thereby converting the methane to C2 hydrocarbons at a methane conversion of greater than 20% and a C2 selectivity of greater than 50%.97. The method of claim 96 , wherein the method produces a product gas comprising less than 0.5% carbon monoxide. This invention is generally related to novel catalysts and, more specifically, to doped metal oxide catalysts useful as heterogeneous catalysts in a variety of catalytic reactions, such as the oxidative coupling of methane to C2 hydrocarbons.Catalysis is the process in which the rate of a chemical reaction is either increased or decreased by means of a catalyst. Positive catalysts increase the speed of a chemical reaction, ...

Catalyst and Process for Olefin Metathesis Reaction

The present invention relates to a magnesium oxide (MgO) catalyst for isomerisation of olefins with defined physical properties. The present invention further relates to a catalyst for conversion of olefins having a first catalyst component and a second catalyst component. The first catalyst component has a metathesis catalyst. The second catalyst component has the magnesium oxide catalyst. A process for obtaining an olefin is also disclosed.

Multistage Nanoreactor Catalyst and Preparation and Application Thereof

The present disclosure discloses a multistage nanoreactor catalyst and preparation and application thereof, belonging to the technical field of synthesis gas conversion. The catalyst consists of a core of an iron-based Fischer-Tropsch catalyst, a transition layer of a porous oxide or porous carbon material, and a shell layer of a molecular sieve having an aromatization function. The molecular sieve of the shell layer can be further modified by a metal element or a non-metal element, and the outer surface of the molecular sieve is further modified by a silicon-oxygen compound to adjust the acidic site on the outer surface and the aperture of the molecular sieve, thereby inhibiting the formation of heavy aromatic hydrocarbons. According to the disclosure, the shell layer molecular sieve with a transition layer and a shell layer containing or not containing auxiliaries, and with or without surface modification can be prepared by the iron-based Fischer-Tropsch catalyst through multiple steps. The catalyst can be used for direct preparation of aromatic compounds, especially light aromatic compounds, from synthesis gas; the selectivity of light aromatic hydrocarbons in hydrocarbons can be 75% or above, and the content in the liquid phase product is not less than 95%; and the catalyst has good stability and good industrial application prospect. 1. A method for preparing a multistage nanoreactor catalyst , comprising the following steps:step 1, impregnating a prepared iron-based catalyst into an organic solvent containing a transition layer oxide precursor, continuously stirring for 0 to 24 h, then performing rotary evaporation to remove the organic solvent and drying at 30 to 250° C. for 0 to 24 h to obtain a sample;step 2, impregnating the sample prepared in step 1 into an alkaline solution containing a template, a silicon source and an aluminum source, and stirring for 0 to 24 h, wherein weight ratio of the sample, the template, the silicon source, the aluminum source, ...

Sabatier process and apparatus for controlling exothermic reaction

A Sabatier process involving contacting carbon dioxide and hydrogen in a first reaction zone with a first catalyst bed at a temperature greater than a first designated temperature; feeding the effluent from the first reaction zone into a second reaction zone, and contacting the effluent with a second catalyst bed at a temperature equal to or less than a second designated temperature, so as to produce a product stream comprising water and methane. The first and second catalyst beds each individually comprise an ultra-short-channel-length metal substrate. An apparatus for controlling temperature in an exothermic reaction, such as the Sabatier reaction, is disclosed.

PROCESS FOR PRODUCING ETHYLENE FROM AN ETHANOL FEEDSTOCK

A process for producing ethylene from an ethanol feedstock comprises a step of subjecting the ethanol feedstock to a dehydration reaction in the presence of a supported heteropolyacid salt catalyst. The supported heteropolyacid salt catalyst includes a support and a heteropolyacid salt compound which is carried on the support and which is represented by a formula as defined herein. 1. A process for producing ethylene from an ethanol feedstock , comprising a step of subjecting the ethanol feedstock to a dehydration reaction in the presence of a supported heteropolyacid salt catalyst.wherein the supported heteropolyacid salt catalyst is prepared from a supported heteropolyacid catalyst which includes a support and a heteropolyacid carried on the support with a weight ratio of the heteropolyacid to the support in a range from 0.1:1 to 2.5:1; and [{'br': None, 'sup': a', 'a', 'd, 'sub': n', '4-n', '12', '40, '(MH)XMO\u2003\u2003Formula 1,'}, {'br': None, 'sup': b', 'b', 'e, 'sub': q', '3-q', '12', '40, '(MH)XMO\u2003\u2003Formula 2, and'}, {'br': None, 'sup': c', 'c', 'f, 'sub': p', '6-p', '18', '62, '(MH)XMO\u2003\u2003Formula 3,'}], 'wherein the supported heteropolyacid salt catalyst includes a support and a heteropolyacid salt compound which is carried on the support and which is represented by a formula selected from the group consisting of'}wherein:{'sup': a', 'b', 'c, 'M, M, and Mare independently selected from the group consisting of Cu, Ag, Au, Zn, Cd, and Hg;'}{'sup': 'a', 'Xis selected from the group consisting of Si and Ge;'}{'sup': b', 'c, 'Xand Xare independently selected from the group consisting of P and As;'}{'sup': d', 'e', 'f, 'M, M, and Mare independently selected from the group consisting of Mo and W;'}n is an integer ranging from 1 to 4;q is an integer ranging from 1 to 3; andp is an integer ranging from 1 to 6.2. The process according to claim 1 , wherein the dehydration reaction is performed at a temperature ranging from 180° C. to 450° C.3. The ...

Catalyst and method for aromatization of c3-c4 gases, light hydrocarbon fractions and aliphatic alcohols, as well as mixtures thereof

The invention relates to hydrocarbon feedstock processing technology, in particular, to catalysts and technology for aromatization of C 3 -C 4 hydrocarbon gases, light low-octane hydrocarbon fractions and oxygen-containing compounds (C 1 -C 3 aliphatic alcohols), as well as mixtures thereof resulting in producing an aromatic hydrocarbon concentrate (AHCC). The catalyst comprises a mechanical mixture of 2 zeolites, one of which is characterized by the silica/alumina ratio SiO 2 /Al 2 O 3 =20, pre-treated with an aqueous alkali solution and modified with oxides of rare-earth elements used in the amount from 0.5 to 2.0 wt % based on the weight of the first zeolite. The second zeolite is characterized by the silica/alumina ratio SiO 2 /Al 2 O 3 =82, comprises sodium oxide residual amounts of 0.04 wt % based on the weight of the second zeolite, and is modified with magnesium oxide in the amount from 0.5 to 5.0 wt % based on the weight of the second zeolite. Furthermore, the zeolites are used in the weight ratio from 1.7:1 to 2.8:1, wherein a binder comprises at least silicon oxide and is used in the amount from 20 to 25 wt % based on the weight of the catalyst. The process is carried out using the proposed catalyst in an isothermal reactor without recirculation of gases from a separation stage, by contacting a fixed catalyst bed with a gaseous feedstock, which was evaporated and heated in a preheater. In The technical result consists in achieving a higher aromatic hydrocarbon yield while ensuring almost complete conversion of the HC feedstock and oxygenates, an increased selectivity with respect to forming xylols as part of an AHCC, while simultaneously simplifying the technological setup of the process by virtue of using a reduced (inter alia, atmospheric) pressure.

MULTIMETALLIC MIXED OXIDES, ITS PREPARATION AND USE FOR THE OXIDATIVE DEHYDROGENATION OF ETHANE FOR PRODUCING ETHYLENE

A layered multimetallic mixed oxide (LMMO) is characterized by one or more diffraction peaks at 5<2θ<15, preferably between 10<2θ<15. The catalysts can be represented by the general formula: 113-. (canceled)14. A process for preparing a nanometer and micrometer layered multimetallic oxide catalyst having the formula{'br': None, 'sub': 'δ', 'M1 M2 M3 O'}wherein:M1 is selected from the group of Ag, Au, Zn, Sn, Rh, Pd, Pt, Cu, Ni, Fe, Co, an alkaline metal, an alkaline earth metal, a rare earth metal, and mixtures thereof;M2 is selected from the group of Ti, Hf, Zr, Sn, Bi, Sb, V, Nb, Ta and P, and mixtures thereof;M3 is selected from the group of Mo, W and Cr, and mixtures thereof;and where said multilayered metallic oxide exhibits a major X-ray diffraction peak between 5<2θ<15,said process comprising the steps of{'sub': 1', '2', '3, 'mixing metallic precursors of M, Mand Mto form a precursor mixture,'}hydrothermal treatment of the resulting mixture to obtain a homogeneous solid mixture, andthermally treating the solid mixture to activate the solid mixture and obtain said catalyst.15. The process of claim 14 , whereinthe precursors are mixed by mechanical mixing or by dissolution of the corresponding metal salts.17. The process of claim 14 , further comprising the steps ofadding a chemical agent to the precursor mixture selected from the group consisting of an amino acid, glycine, amines, urea or carboxylic acids, or a mixture thereof.18. The process of claim 14 , whereinsaid precursors are selected from the group consisting of pure metallic elements, metallic salts, metallic oxides, metallic hydroxides, metallic alkoxides, acids, and mixtures thereof.19. The process of claim 18 , whereinsaid precursors are selected from the group consisting of nitrates, oxalates, sulfates, carbonates, halides, and mixtures thereof.20. The process of claim 14 , whereinsaid catalyst exhibits at least one X-ray diffraction pattern selected from the group consisting of monoclinic lattice ...

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 % ...

FIXED BED RADIAL FLOW REACTOR FOR LIGHT PARAFFIN CONVERSION

Systems and methods are provided for conversion of light paraffinic gases to form liquid products in a process performed in a fixed bed radial-flow reactor. The light paraffins can correspond to C paraffins. Examples of liquid products that can be formed include C-Caromatics, such as benzene, toluene, and xylene. The fixed bed radial-flow reactor can allow for improved control over the reaction conditions for paraffin conversion in spite of the fixed bed nature of the reactor. This can allow the process to operate with improved efficiency while reducing or minimizing the complexity of operation relative to non-fixed bed reactor systems. 112.-. (canceled)13. A method for processing a paraffin-containing feed , comprising:{'sub': 3+', '6', '12, 'exposing a feed comprising about 30 vol % to about 70 vol % of C paraffins to one or more fixed beds of a conversion catalyst to form a conversion effluent comprising C-Caromatics, the one or more fixed beds of the conversion catalyst comprising fixed beds in one or more radial flow reactors, a combined pressure drop across the one or more fixed beds being less than about 100 kPag, the one or more radial flow reactors comprising{'b': '1', 'an outer annular volume defined by an interior of a reactor wall and an exterior of a gas-permeable wall, the interior of the reactor wall defining an outer annular radius R;'}{'b': '3', 'a central volume defined by the interior of a central column and a column cap, the interior of the central column defining a column radius R; and'}{'b': '2', 'an inner annular volume defined by an interior of the gas-permeable wall, an exterior of the central column, an inner annular top, and an inner annular bottom, the interior of the gas-permeable wall defining an inner annular radius R, the inner annular volume comprising a catalyst bed, the inner annular volume being in direct fluid communication with the outer annular volume through the gas-permeable wall, the inner annular volume being in direct ...

CATALYST BASED ON CATECHOLAMINE AND ITS USE IN A HYDROTREATMENT AND/OR HYDROCRACKING PROCESS

The invention concerns a catalyst comprising a support based on alumina or silica or silica-alumina, at least one element selected from group VIII and/or group VIB, and at least one catecholamine. The invention also concerns the process for the preparation of said catalyst and its use in a hydrotreatment and/or hydrocracking process. 1. A catalyst comprising a support based on alumina or silica or silica-alumina , at least one element selected from group VIII and/or group VIB , and at least one catecholamine.2. The catalyst as claimed in claim 1 , in which the catecholamine is selected from dopamine claim 1 , noradrenaline claim 1 , adrenaline and isoprenaline claim 1 , alone or as a mixture.3. The catalyst as claimed in claim 1 , in which the content of the element from group VIB is in the range 5% to 40% by weight claim 1 , expressed as the oxide of the metal from group VIB with respect to the total weight of catalyst claim 1 , and the content of the element from group VIII is in the range 1% to 10% by weight claim 1 , expressed as the oxide of the metal from group VIII with respect to the total weight of catalyst.4. The catalyst as claimed in claim 1 , further containing phosphorus claim 1 , the quantity of phosphorus being in the range 0.01% to 20% by weight claim 1 , expressed as POwith respect to the total weight of catalyst claim 1 , and the ratio of phosphorus to the element from group VIE in the catalyst being greater than or equal to 0.01.5. The catalyst as claimed in claim 1 , in which the quantity of catecholamine is in the range 1% to 40% by weight with respect to the weight of the support.6. The catalyst as claimed in claim 1 , further containing an organic compound other than catecholamine claim 1 , containing oxygen and/or nitrogen and/or sulphur.7. The catalyst as claimed in claim 6 , in which the organic compound is selected from a compound comprising one or more chemical functions selected from a carboxyl claim 6 , alcohol claim 6 , thiol claim 6 ...

Activation of Dehydrogenation Catalysts

In a process for dehydrogenating cyclohexylbenzene and/or alkyl-substituted cyclohexylbenzene compounds, a dehydrogenation catalyst comprising at least one Group 10 metal compound on a support is heated in the presence of hydrogen from a first temperature from 0° C. to 200° C. to a second, higher temperature from 60° C. to 500° C. at a ramp rate no more than 100° C./hour. The dehydrogenation catalyst is contacted with hydrogen at the second temperature for a time from 3 to 300 hours to produce an activated dehydrogenation catalyst. A feed comprising cyclohexylbenzene and/or an alkyl-substituted cyclohexylbenzene compound is then contacted with hydrogen in the presence of the activated dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising biphenyl and/or an alkyl-substituted biphenyl compound. 1. A process for dehydrogenating cyclohexylbenzene and/or alkyl-substituted cyclohexylbenzene compounds , the process comprising:(a) providing a dehydrogenation catalyst comprising at least one Group 10 metal compound on a support;(b) heating the dehydrogenation catalyst in the presence of hydrogen from a first temperature from 0° C. to 200° C. to a second, higher temperature from 60° C. to 500° C. at a ramp rate no more than 100° C./hour;(c) contacting the dehydrogenation catalyst with hydrogen at the second temperature for a time from 3 to 300 hours to produce an activated dehydrogenation catalyst; and(d) contacting a feed comprising cyclohexylbenzene and/or an alkyl-substituted cyclohexylbenzene compound with hydrogen in the presence of the activated dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising biphenyl and/or an alkyl-substituted biphenyl compound.2. The process of claim 1 , wherein the at least one Group 10 metal comprises platinum.3. The process of claim 1 , wherein the dehydrogenation catalyst comprises from 0.1 to 5% wt % of elemental platinum.4. The ...

DUAL CATALYST SYSTEM FOR PROPYLENE PRODUCTION

Embodiments of processes for producing propylene utilize a dual catalyst system comprising a mesoporous silica catalyst impregnated with metal oxide and a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm/g, and the MFI structured silica catalyst has a total acidity of 0.001 mmol/g to 0.1 mmol/g. The propylene is produced from the butene stream via metathesis by contacting the mesoporous silica catalyst and subsequent cracking by contacting the MFI structured silica catalyst. 1. A dual catalyst system for producing propylene from butene , the dual catalyst system comprising a metathesis catalyst zone and a cracking catalyst zone downstream of the metathesis catalyst zone where:{'sup': '3', 'the metathesis catalyst zone comprises mesoporous silica catalyst impregnated with metal oxide, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm/g; and'}the cracking catalyst zone comprises a mordenite framework inverted (MFI) structured silica catalyst, where the MFI structured silica catalyst includes a pore size distribution of at least 1.5 nm to 3 nm, and a total acidity of 0.001 mmol/g to 0.1 mmol/g.2. The dual catalyst system of where the metathesis catalyst zone and the cracking catalyst zone are disposed in one reactor.3. The dual catalyst system of where the metathesis catalyst zone is disposed in a first reactor and the cracking catalyst zone is disposed in a second reactor downstream of the first reactor.4. The dual catalyst system of further comprising a conduit between the first reactor and the second reactor.5. The dual catalyst system of where the metal oxide of the mesoporous silica catalyst comprises one or more oxides of molybdenum claim 1 , rhenium claim 1 , tungsten ...

Process of Making Olefins or Alkylate by Reaction of Methanol and/or DME or by Reaction of Methanol and/or DME and Butane

Methods of simultaneously converting butanes and methanol to olefins over Ti-containing zeolite catalysts are described. The exothermicity of the alcohols to olefins reaction is matched by endothermicity of dehydrogenation reaction of butane(s) to light olefins resulting in a thermo-neutral process. The Ti-containing zeolites provide excellent selectivity to light olefins as well as exceptionally high hydrothermal stability. The coupled reaction may advantageously be conducted in a staged reactor with methanol/DME conversion zones alternating with zones for butane(s) dehydrogenation. The resulting light olefins can then be reacted with iso-butane to produce high-octane alkylate. The net result is a highly efficient and low cost method for converting methanol and butanes to alkylate. 1. A method of producing alkylate , comprising:passing methanol and/or dimethylether (DME) into a reaction chamber;passing butane into the reaction chamber;{'sub': 4', '4, 'wherein the reactor comprises a catalyst that is a crystalline zeotype material in which tetrahedral [TiO] and [SiO] units are arranged in a MFI structure with a three-dimensional system of channels having a molecular dimension of 4.9 to 5.9 A, preferably 5.1-5.6 Å, and at least 0.5 mass % Ti, more preferably at least 1% Ti, in some embodiments in the range of 1 to 5 mass %Ti;'}reacting the methanol and/or DME and the butane in the reaction chamber in the presence of the catalyst to make olefins under steady state conditions where the reaction is adiabatic or nearly adiabatic such that +/−200 kJ/(kg olefin produced) or less is transferred from the reaction chamber (preferably +/−100 or less, more preferably +/−50, and preferably +/−10 kJ/(kg olefin produced) or less is transferred from the reaction chamber; andreacting the olefins with iso-butane to form alkylate in a separate reactor.2. The method of where reaction chamber further comprises a second catalyst comprising at least 1 claim 1 , or at least 2 claim 1 , or ...

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: ...

Methods for alkane dehydrogenation

Disclosed herein are methods for dehydrogenation of alkanes to olefins by co-injecting the alkane feed with hydrogen. The present methods provide the improved feed conversion, desired product selectivity, total olefins in product stream, and lower catalyst deactivation rate.

METHOD FOR PRODUCTION OF CONJUGATED DIOLEFIN

An object of the present invention is to provide a method for production of a high purity conjugated diolefin. The method for production of a conjugated diolefin of the present invention comprises steps of supplying a source gas containing a C4 or higher monoolefin and an oxygen-containing gas into a reactor, bringing a catalyst into contact with the gas mixture, compressing a gas containing a conjugated diolefin produced by an oxidative dehydrogenation reaction to obtain a liquefied gas and rinsing the liquefied gas with water. 1. A method for production of a conjugated diolefin comprising steps of supplying a source gas containing a C4 or higher monoolefin and an oxygen-containing gas into a reactor , bringing a catalyst into contact with the gas mixture , compressing a gas containing a conjugated diolefin produced by an oxidative dehydrogenation reaction to obtain a liquefied gas and rinsing the liquefied gas with water.2. The method for production of the conjugated diolefin according to claim 1 , further comprising steps of:cooling the gas containing the conjugated diolefin, andallowing the gas containing the conjugated diolefin to be absorbed in a solvent, followed by stripping the gas containing the conjugated diolefin from the solvent.3. The method for production of the conjugated diolefin according to comprising the following steps of (1) to (6) in this order:step (1): a step of supplying a source gas containing a C4 or higher monoolefin and an oxygen-containing gas into a reactor and bringing a catalyst into contact with the gas mixture to obtain a gas containing a conjugated diolefin by an oxidative dehydrogenation reaction,step (2): a step of cooling the gas containing the conjugated diolefin in a quench column,step (3): a step of allowing the gas containing the conjugated diolefin to be absorbed in a solvent, subsequently stripping the gas containing the conjugated diolefin from the solvent, followed by compressing the gas to obtain a liquefied gas,step ...