СПОСОБ ПОЛУЧЕНИЯ ЛИНЕЙНЫХ АЛКИЛБЕНЗОЛОВ

Изобретение относится к способу получения линейных алкилбензолов, которые являются полупродуктами и используются в производстве моющих средств. Описывается способ получения линейных алкилбензолов, содержащих от 10 до 14 атомов углерода в алкильной цепи, включающий следующий цикл операций: а) дигидрогенизацию С10-С14 н-парафинов до соответствующих н-олефинов в реакторе дегидрогенизации с получением смеси, содержащей также диолефины и ароматические побочные продукты, а также легкие продукты разложения и водород, б) селективную гидрогенизацию диолефинов, полученных в операции (а), до моноолефинов, с получением смеси, состоящей по существу из моноолефинов и н-парафинов в дополнение к ароматическим побочным продуктам, полученным в операции (а); в) подачу потока, поступающего с операции (б), вместе с потоком, состоящим из бензола, в аппарат алкилирования, в котором присутствует катализатор алкилирования; г) подачу продукта алкилирования в секцию дистилляции для выделения, соответственно, избытка ...

НОВЫЙ СПОСОБ ПРОИЗВОДСТВА МЕТАНОЛА ИЗ НИЗКОКАЧЕСТВЕННОГО СИНТЕТИЧЕСКОГО ГАЗА

Настоящее изобретение относится к способу производства метанола из синтетического газа, а также к компоновке реактора для его осуществления. Способ включает следующие стадии: - предоставление свежего сжатого газа для синтеза метанола, содержащего водород, монооксид углерода и диоксид углерода, который предварительно нагревают и пропускают через адиабатический метанольный предварительный конвертер/предохранительный реактор, в котором синтетический газ частично конвертируют в метанол в присутствии гетерогенного метанольного катализатора, а ядовитые примеси из подаваемого газа удаляют, - предоставление рециркуляционного газового потока из схемы синтеза, содержащего частично конвертированный газ для синтеза метанола, и смешивание части рециркуляционного газового потока со свежим синтетическим газом, если это необходимо, как в случае частичной загрузки, с получением потока технологического газа, - охлаждение потока технологического газа из предварительного конвертера/предохранительного реактора ...

ПОЛУЧЕНИЕ НИЗКОМОЛЕКУЛЯРНЫХ ОЛЕФИНОВ ИЗ СИНТЕЗ-ГАЗА

Изобретение относится к вариантам способа получения низкомолекулярных олефинов путем конверсии сырьевого потока, содержащего монооксид углерода и водород, с применением нанесенного катализатора на основе железа, в котором обеспечивают каталитическую композицию, содержащую железосодержащие частицы, диспергированные на подложке, которая содержит α-оксид алюминия (α-AlO), причем указанная подложка содержит по меньшей мере 1 масс. % (в пересчете на массу подложки) железосодержащих частиц, и основная часть железосодержащих частиц находится в непосредственном контакте с α-оксидом алюминия. Также изобретение относится к способу получения указанной композиции и применению катализатора, полученного данным способом. Настоящее изобретение позволяет повысить селективность к образованию низкомолекулярных олефинов и снизить селективность по отношению к образованию нежелательного метана. 4 н. и 20 з.п. ф-лы, 4 табл., 5 пр., 5 ил.

ОБЪЕДИНЕННЫЙ СПОСОБ ПРОИЗВОДСТВА КУМОЛА

Использование: нефтехимия. Сущность: объединенный способ получения кумола включает дегидрирование потока пропана в пропилен на установке дегидрирования и направление потока, выходящего из установки дегидрирования и содержащего 25-40 мас.% пропилена, в установку алкилирования вместе с потоком бензола при мольном отношении бензол/пропилен в интервале от 8 до 10. Продукт алкилирования перегоняют на первой ректификационной колонне для выделения легкой фракции, по существу, состоящей из пропана, которую возвращают на повторный цикл дегидрирования, и тяжелой фракции, которую перегоняют на второй ректификационной колонне для выделения с верха колонны непрореагировавшего бензола, который возвращают на повторный цикл на установку алкилирования, и кумола с чистотой свыше 99% с нижней части колонны. Технический результат: расширение арсенала технических средств получения кумола. 5 з.п.ф-лы, 1 ил.

СПОСОБ ПРОИЗВОДСТВА МЕТАНОЛА, ДИМЕТИЛОВОГО ЭФИРА И НИЗКОУГЛЕРОДИСТЫХ ОЛЕФИНОВ ИЗ СИНТЕЗ-ГАЗА

Настоящее изобретение обеспечивает процесс производства метанола, диметилового эфира как основных продуктов и низкоуглеродистого олефина как побочного продукта из синтез-газа, в котором указанный процесс содержит стадию контакта синтез-газа с катализатором. Катализатор содержит аморфный сплав, состоящий из первого компонента А1 и второго компонента, при этом указанный второй компонент является одним или несколькими элементами или их окислами, выбранными из группы IA, IIIА, IVA, VA, IB, IIВ, IVB, VB, VIB, VIIB, VIII и ряда лантанидов периодической таблицы элементов, при этом указанный второй компонент отличается от первого компонента А1. Условия для преобразования имеют температуру реакции 200-270°C, давление реакции 1-6 МПа, объемную скорость подачи синтез-газа 1000-10000 мл/г·час и мольное отношение между Ни CO в синтез-газе от 1 до 3. Согласно настоящему процессу синтез-газ может быть преобразован в метанол, диметиловый эфир и низкоуглеродистый олефин с высокой степенью преобразования ...

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.

ВОЗОБНОВЛЯЕМАЯ УГЛЕВОДОРОДНАЯ КОМПОЗИЦИЯ

Изобретение относится к углеводородной композиции. Углеводородная композиция, пригодная в качестве топлива или топливного компонента, содержит от 10 до 40 масс.% неразветвленных C-алканов, от 0,1 до 15 масс.% ароматических C-углеводородов, из которых, по меньшей мере, 90 масс.% являются моноароматическими, и не более чем 1 масс.% в сумме кислородсодержащих соединений; причем в данной композиции суммарное содержание C-алканов составляет от 50 до 95 масс.%, а суммарное содержание C-алканов, ароматических C-углеводородов и C-циклоалканов составляет, по меньшей мере, 95 масс.%; и данные количества вычислены по отношению к массе композиции. Кроме того, заявлен способ изготовления композиции, ее применение и смешанное топливо. Технический результат – получение углеводородной композиции, которую можно использовать в качестве топливного компонента или топлива. Малое содержание кислородсодержащих компонентов в составе композиции обеспечивает устойчивость при хранении и меньшую разрушаемость автомобильных ...

ФОСФОРСОДЕРЖАЩИЙ КАТАЛИЗАТОР ДЛЯ ПРЕВРАЩЕНИЯ ОКСИГЕНАТОВ В ОЛЕФИНЫ

Изобретение относится к способу приготовления фосфорсодержащего катализатора, включающему следующие стадии: (a) экструдирование смеси, которая содержит цеолит и оксид алюминия или гидрат оксида алюминия, в качестве связующего, (b) кальцинирование полученного на стадии (а) экструдата, (c) обработка полученного на стадии (b) кальцинированного экструдата водяным паром, (d) нанесение фосфорсодержащего соединения на обработанный водяным паром экструдат со стадии (с) и (e) кальцинирование модифицированного фосфором экструдата со стадии (d), причем массовая доля фосфора в полученном после стадии (е) катализаторе составляет от 0,8 до 2,5 мас. %. Также изобретение относится к катализатору превращения оксигенатов в олефины, способу получения олефинов из оксигенатов и применению катализатора для превращения оксигенатов в олефины. Получаемый катализатор обладает увеличенным сроком службы при остающейся неизменно селективности и увеличенной степени превращения. 4 н. и 14 з.п. ф-лы, 7 ил., 2 табл., 7 ...

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.

СПОСОБ ДЕГИДРИРОВАНИЯ ЭТИЛБЕНЗОЛА ДО СТИРОЛА

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

КАТАЛИЗАТОР ИЗБИРАТЕЛЬНОГО ГИДРИРОВАНИЯ НЕНАСЫЩЕННЫХ СОЕДИНЕНИЙ И СПОСОБ ИЗБИРАТЕЛЬНОГО ГИДРИРОВАНИЯ НЕНАСЫЩЕННЫХ СОЕДИНЕНИЙ

Объектом изобретения является катализатор избирательного гидрирования ненасыщенных соединений на основе благородного металла и/или окиси благородного металла на окиси алюминия, который в исходном состоянии имеет следующую характеристику диафракции рентгеновских лучей: Данный катализатор получают за счет того, что благородный металл в виде водного раствора его соли вводят в окись алюминия. 2 с.п. и 5 з.п. ф-лы, 3 табл., 2 ил.

КАТАЛИЗАТОР ДЛЯ КОНВЕРСИИ СИНТЕЗ-ГАЗА В УГЛЕВОДОРОДЫ И СПОСОБ ПОЛУЧЕНИЯ УГЛЕВОДОРОДОВ

Сущность изобретения: продукт - катализатор состава, %: кобальт 3-60; рений 0,03-18,00; оксид алюминия остальное, причем содержание рения в катализаторе составляет 1-30 мас.% относительно содержания кобальта. Катализатор может дополнительно содержать оксид щелочного металла в количестве 0,5-5,0 ат. % относительно содержания кобальта и/или 0,1-5,0 мас.% оксида металла, выбранного из группы оксидов циркония, ванадия и РЗЭ. Катализатор получают пропиткой носителя солями указанных металлов с последующей сушкой и прокаливанием. Другим продуктом являются углеводороды, которые получают при 190-280°С, давлении 1-40 ат, объемной скорости синтез-газа 100-10000 см3/г кат. в час при молярном соотношении между водородом и оксидом углерода от 1:1 до 2,5:1 на катализаторе приведенного состава. При этом процесс проводят в суспензионном реакторе предпочтительно при молярном соотношении между водородом и оксидом углерода 1,5:1-2,5:1. Характеристика: повышенная активность и селективность катализатора, приводящая ...

СПОСОБ КОНВЕРСИИ ГАЗООБРАЗНЫХ УГЛЕВОДОРОДОВ В ОЛЕФИНЫ

... 1. Способ конверсии газообразных углеводородов в олефины, отличающийся тем, что нагревают подаваемый поток, содержащий алкан и окислитель, до температуры приблизительно от 75 до 800°С, достаточной для инициирования окислительного дегидрирования алкана, затем проводят контактирование подаваемого потока с катализатором, присутствующим в неподвижном слое и включающим основной металл, промотирующий металл и носитель, содержащий множество дискретных структур, при этом поддерживают время контактирования алкана с катализатором менее 200 мс и поддерживают условия, необходимые для окислительного дегидрирования. 2. Способ по п.1, отличающийся тем, что используют окислитель, который включает кислородсодержащий газ. 3. Способ по п.2, отличающийся тем, что используют окислитель представляющий собой по существу чистый кислород. 4. Способ по п.1, отличающийся тем, что подаваемый поток нагревают до температуры ниже 700°С. 5. Способ по п.1, отличающийся тем, что подаваемый поток нагревают до температуры ...

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 ...

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 УВЕЛИЧЕНИЯ ВЫХОДА ИЗ ЗОНЫ ИЗОМЕРИЗАЦИИ

Изобретение относится к способу увеличения выхода из зоны изомеризации, который включает отделение части Сциклических углеводородов от потока нафты, содержащего Суглеводороды, для получения потока, обедненного по Сциклическим углеводородам; отделение изоCуглеводородов, изоCуглеводородов и изоCуглеводородов от потока, обедненного по Сциклическим углеводородам; и направление по меньшей мере одного потока, обогащенного по изоСуглеводородам, изоCуглеводородам, изоCуглеводородам или их комбинации, в зону изомеризации. Способ позволяет эффективно и действенно превращать изоуглеводороды в нормальные парафины в одной и той же зоне изомеризации. 9 з.п. ф-лы, 1 ил., 1 табл.

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 ...

КАТАЛИЗАТОР ДЛЯ ПИРОЛИЗА СЫРЬЯ

МЕЗОПОРИСТЫЙ И МАКРОПОРИСТЫЙ КАТАЛИЗАТОР НА ОСНОВЕ НИКЕЛЯ, ПОЛУЧЕННЫЙ СОВМЕСТНЫМ ПЛАСТИЦИРОВАНИЕМ И ИМЕЮЩИЙ МЕДИАННЫЙ ДИАМЕТР МАКРОПОР, ПРЕВЫШАЮЩИЙ 300 НМ, И ЕГО ПРИМЕНЕНИЕ ПРИ ГИДРИРОВАНИИ УГЛЕВОДОРОДОВ

СМЕСИ ИЗОМЕРОВ (МЕТИЛЦИКЛОГЕКСИЛ)ТОЛУОЛА, ИХ ПОЛУЧЕНИЕ И ИХ ПРИМЕНЕНИЕ ДЛЯ ПОЛУЧЕНИЯ ПЛАСТИФИКАТОРОВ

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 ...

СПОСОБ ДЕКАРБОКСИЛИРУЮЩЕЙ КЕТОНИЗАЦИИ ЖИРНЫХ КИСЛОТ ИЛИ ПРОИЗВОДНЫХ ЖИРНОЙ КИСЛОТЫ

СПОСОБ АЛКИЛИРОВАНИЯ С ИСПОЛЬЗОВАНИЕМ ЦЕОЛИТА UZM-8

... 1. Способ алкилирования для получения моноалкилированного ароматического соединения, включающий: ! а) пропускание ароматического исходного материала, содержащего исходное ароматическое соединение, олефинового исходного материала, содержащего ! C2-C4олефин, и дополнительного потока, содержащего алкилированное производное исходного ароматического соединения, содержащее от одной до шести дополнительных C2-C4адкильных групп в сравнении с исходным ароматическим соединением, через слой катализатора алкилирования, содержащий твердый катализатор, где твердый катализатор содержит микропористый кристаллический цеолит, имеющий слоистую структуру по меньшей мере из тетраэдрических единиц ! AlO2 и SiO2 и состав, на основе синтезированного безводного продукта, выраженный эмпирической формулой ! Mm n+Rr p+Al1-xExSiyOz, ! где М обозначает по меньшей мере один обмениваемый катион, "m" обозначает отношение М к (Al+Е) и варьируется от 0 до 2,0, R обозначает по меньшей мере один аммонийорганический катион, ...

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 катализатора для изомеризации углеводородов

Способ получения парафиновых и олефиновых углеводородов

Способ получения насыщенных карбо-или гетероциклических соединений

Катализатор для измеризации углеводородов с @ -с @

Способ получения изопрена

Verfahren zur Alkylierung der Seitenkette alkylsubstituierter aromatischer Kohlenwasserstoffe

Verfahren zur Herstellung von Olefinen und Wasserstoff sowie Katalysator

Katalysator zur selektiven Hydrierung von Acetylen

VERFAHREN ZUR HERSTELLUNG VON OLEFINISCH UNGESAETTIGTEN ALIPHATISCHEN ODER CYCLOALIPHATISCHEN KOHLENWASSERSTOFFEN

VERFAHREN ZUR HERSTELLUNG VON AETHAN DURCH SELEKTIVE HYDROGENOLYSE VON ALKANEN

Production of propene and 1-butene

Production of propene and 1-butene comprises reading 2-pentene with ethene in the presence of a metathesis catalyst containing a VIb, VIIb or VIIIb metal. An apparatus for carrying out the process is also claimed comprising a metathesis reactor (R1) to react 1-butene with 2-butene, connected to a distillation column (D1) to separate 2-3C light boiling, 4C middle boiling and 5C high boiling phases. The light boiling outlet loads to a column (D3) for separating ethene and propene, the middle boiling outlet leads to the reactor (R1) or is discharged, and the high boiling outlet leads to a reactor (R2) for reacting 2-pentene with ethene, whose outlet leads into a column (D1). The ethene outlet from the column (D3) and an ethene feed are led to the reactor (R2).

Verfahren zur flexiblen Herstellung von Propen und Hexen

KATALYSATOR FUER DIE HERSTELLUNG VON AETHYLEN

FISCHER-TROPSCH CONVERSION OF SYNTHESIS GAS TO HYDROCARBONS

HETEROGENES ISOPARAFFIN/OLEFIN-ALKYLIERUNGSVERFAHREN.

Process for the preparation of but-2-yne

... 1,2-Butadiene is subjected to a rearrangement reaction using a finely-divided metallic alkali metal on a support to give but-2-yne. This reaction proceeds under comparatively mild conditions with high selectivity and high yield.

UMWANDLUNG EINES NIEDRIGEN ALKANS.

Verfahren zur Umwandlung von Toluol und Butadien in Styrol und 1-Penten.

Verfahren zur Umwandlung von Methanol zu flüssigen Kohlenwasserstoffen.

Verfahren zur Olenfinethylierung

Verfahren zur Herstellung eines verzweigten Olefins, Verfahren zur Verwendung des verzweigten Olefins zur Herstellung eines Tensids

Verfahren zur Herstellung von Cyclohexan

Dehydrierkatalysator

VERFAHREN ZUR DOPPELBINDUNGSISOMERISIERUNG VON ALKENEN

KUGELFOERMIGE KATALYSATOREN ZUR HERSTELLUNG VON METHAN

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

IN SITU VERRINGERUNG DER VERKOKUNG EINES PORÖSEN KATALYSATORS IN EINEM SUPERKRITISCHEN REAKTIONSMEDIUM

Rhenium-enthaltender Metathesekatalysator, Verfahren zu seiner Herstellung und seine Verwendung

FORTSCHREITEN IN DER DEHYDRIERUNGSKATALYSE

PROCESS FOR THE PREPARATION OF HYDROCARBONS

Verfahren zur Hydrierung von Kohlenoxyd zu mehrgliedrigen Kohlenwasserstoffen

KATALYSATOREN AUF GAMMA -ALUMINIUMOXIDBASIS ZUR ENTALKYLIERUNG AROMATISCHER KOHLENWASSERSTOFFE MIT WASSER

Metathesis of olefinic cuts comprises use of catalyst comprising delta-aluminum oxide, rhenium and cesium

Metathesis of an olefinic 5C cut uses a catalyst comprising delta -aluminum oxide, rhenium and cesium.

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

Verfahren zur katalytischen Disproportionierung acyclischer Olefine

Verfahren und Vorrichtung zur Dampf-Dealkylierung in einer Anlage zur katalytischen Reformierung von Kohlenwasserstoffen

Die vorliegende Erfindung beschreibt ein Verfahren zur Behandlung einer Fraktion, überwiegend bestehend aus Kohlenwasserstoffen mit mindestens sieben Kohlenstoffatomen (C₇₊-Fraktion), wie sie in einer Anlage zur katalytischen Reformierung von kohlenwasserstoffhaltigem Einsatz entsteht, sowie eine Vorrichtung zur Durchführung des Verfahrens. Die C₇₊-Fraktion wird nach einer Hydrierung einer Dampf-Dealkylierung zugeführt, wo die verwertbaren Produkte Benzol und Wasserstoff entstehen.

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.

Isomerisation catalysts for hydrocarbons - contg platinum group metal, halogen and metal halide and rhenium or germanium cpds

The catalysts consists of (A) an alumina carrier, (B) a Pt gp. metal (C) a halogen, (D) a Friedel-Crafts metal halide and (E) a Re or Ge component, the Ge being in an oxidn. stage higher than elementary Ge. Content of Re is pref. 0.01-1 wt % or of Ge pref 0.01-5 wt %, pref. in the form of GeO2. Amount of (B) is pref 0.01-1% and of (C) 0.1-5% (D) is pref. present in amt. of 1-100 wt% of the remaining catalyst. The catalyst may be pre-sulphided to a S content of 0.05-0.5 wt %. They are suitable for isomerisation of olefines, paraffins, cycloparaffins and/or alkyl aromatics, in presence of H2 e.g. in prodn of p-xylene or high octane petrols.

Production of hydrocarbons

In a process for preparing olefins (see Division C5), a halogen substituted paraffin is passed with an olefinically unsaturated hydrocarbon over a halogenated catalyst under conditions such that constituent parts of the halogen substituted paraffin undergo addition across the olefinic bond. Specified olefinic feedstocks are ethylene, propylene, n or iso butenes and halogen substituted paraffins used include chloroform, carbon tetrachloride trichloropropane, and tertiary butyl chloride. The process is carried out at - 30 DEG to + 350 DEG C. preferably in the gaseous or liquid phase in presence of nitrogen as an inert carrier gas and at sub-normal and superatmospheric pressures. In the example, ethylene is bubbled into tertiary butyl chloride while refluxing for two hours in presence of a chlorinated-alumina catalyst to produce (CH3)3 CCH2CH2Cl. Specifications 953,187 and 981,691 are referred to. Reference has been directed by the Comptroller to Specification 921,796.ALSO:Olefins are prepared ...

PRODUCTION OF C7 OLEFINS

... 1,216,278. Heptenes. BRITISH PETROLEUM CO. Ltd. 6 June, 1969 [14 Aug., 1968], No. 38839/68. Heading C5E. C 7 Olefins are obtained by (a) catalytically disproportionating a mixture of butene-1 and butene-2 to yield propylene and pentene-2, and catalytically co-dimerizing the pentene-2 thus obtained with ethylene. Suitable disproportionation catalysts are Mo/Al 2 O 3 Œcobalt oxidesŒ alkali or alkaline earth metals, carbonyls of Mo, W or Re supported on Al 2 O 3 , SiO 2 or Al 2 O 3 / SiO 2 , and preferably Re 2 O 7 /Al 2 O 3 . Suitable codimerization catalysts are alkali or alkaline earth metals or hydrides, and organo-metallic alkali metal compounds and preferably Na or NaH supported on K 2 CO 3 . The feed to step (a) may be an n-butene raffinate stream, which may first be treated by (i) selective hydrogenation to remove dienes and acetylenes, e.g. over a sulphided nickel on sepiolite catalyst, and/or (ii) isomerization to increase the butene-2 content, preferably simultaneously with (i) ...

PROCESS FOR CONVERTING AN OLEFIN TO A PRODUCT CONTAINING HIGHER AND LOWER OLEFINS

... 1386735 Disproportionating C 14 -C 28 olefins GULF RESEARCH & DEVELOPMENT CO 12 Feb 1973 [17 Feb 1972] 6717/73 Heading C5E A mono-olefin having 14 to 28 carbon atoms is disproportionated to give a mixture of olefins of higher and lower carbon number by contact with a catalyst comprising (i) Al 2 O 3 , (ii) Mo or Re and (iii) Ag or Cu at 25-250‹ C. The feed is preferably an -olefin. The Mo or Re may be present in amount 4-12 wt. per cent and the Cu or Ag to amount 0À1-6 wt. per cent based on the total catalyst.

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 ...

Process and catalyst for the hydrogenation of unsaturated hydrocarbons

Unsaturated hydrocarbons or hydrocarbon mixtures are hydrogenated under hydrogen pressure at elevated temperature in the presence of a catalyst comprising a carrier which consists of Al2O3 or of a major proportion of Al2O3 together with another non-acidic carrier material, and a combination of at least one sulphide of tungsten and/or molybdenum and/or rhenium and at least one sulphide of a metal or metals of Group VIII of the Periodic Table, which catalyst during and/or after the convertion of the metal components into sulphides has been treated with hydrochloric acid on precursor therefor. Suitable starting material hydrocarbons are amide benzene and petroleum fractions e.g. boiling in the gasoline, kerosene, gas oil and lubricating oil ranges. Examples describe the hydrogenation of (1) benzene to cyclohexane and (2) kerosene to unspecified products.ALSO:Hydrogenation catalysts are made by drying, calcining and sulphiding particles of Al2O3 or a mixture of a major proportion of Al2O3 and ...

Process for the disproportionation of acyclic olefins

Acyclic olefins and mixtures thereof are dis-proportionated or co-reacted in the presence of a catalyst comprising a mixture of rhenium heptoxide and alumina, the reaction pressure being just sufficient to maintain the reaction product completely in the liquid phase. An inert diluent, e.g. paraffin or cyclo-paraffin, may be present. Examples illustrate the conversion of propylene to ethylene and butene-2.

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.

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.

Production of cycloalkanes

Cycloalkane is added as a diluent in the manufacture of the same cycloalkane from the dicycloalkadiene by thermal depolymerization and catalytic hydrogenation of the resulting monomeric cycloalkadiene. The process is especially suited to the manufacture of cyclopentane. The catalytic hydrogenation of the cycloalkadiene is carried out in a closed loop batch reactor, the catalyst being circulated in the form of a slurry until it is removed from contact with the reactants and reaction product at the end of the reaction by filtration.

Process for the preparation of paraffinic hydrocarbons and of a catalyst for said process

Process for the preparation of paraffins by conversion of naphthenes having the same number of carbon atoms, by contacting the naphthenes in the presence of H2 with a catalyst comprising metallic Pt on an alumina-containing carrier, from which catalyst, prior to said contacting, ionic Pt has been extracted with a solvent which is selective for ionic platinum. A process for the preparation of a catalyst for said process is also claimed. The solvent may be acetylacetone.

DEHYDROGENATION METHOD AND CATALYTIC COMPOSITE FOR USE THEREIN

... 1312708 Dehydrogenation catalyst UNIVERSAL OIL PRODUCTS CO 20 Aug 1970 [21 Aug 1969] 40106/70 Heading B1E [Also in Division C5] A catalyst composition comprises a platinum group component, a germanium component, an alkali metal or alkaline earth metal component, and a porous refractory carrier material. The platinum group component is present as elemental metal in a quantity of 0.01-2 wt%, the germanium is in an oxidation state above that of the metal and in a quantity of 0.01-5 wt% and the alkali or alkaline earth metal is present in a quantity of 0.1 to 5wt%. Specified carriers are (a) refractory oxides, e.g. alumina, titania, zirconia, chromia, zinc oxide, magnesia, thoria, boria, silica-alumina, silica-magnesia, chromia-alumina, aluminaboria, and silica-zirconia, (b) activated carbon. Coke, or charcoal, (c) silica, silica gel, silicon carbide, or clays, e.g. attapulgite, kaolin, diatomaceous earth, fullers earth, (c) ceramics, porcelain, crushed firebrick, or bauxite, or (d) crystalline ...

PROCESS FOR THE PREPARATION OF HYDROCARBONS

PROCESS FOR THE PREPARATION OF FISCHERTROPSCH CATALYSTS

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.

Catalysists for the condensation of oxygenated organic compounds to give hydrocarbons

Novel catalysts resembling zeolites can be prepared by impregnating a microporous glass with a precursor for alumina, alumina/silica or a hydrate thereof and converting the precursor to the desired form. The catalyst permits oxygen-containing organic compounds to be converted into light hydrocarbons with gasoline-boiling products.

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 ...

Catalytic hydrodeoxygenation process

Hydrocarbons containing aluminium compounds and oxygen-containing compounds are purified by first removing the aluminium compounds followed by catalytic hydrogenation. The hydrocarbon may for example be the solvent stripper overhead obtained by stripping the product of oxidizing an aluminium alkyl to the corresponding alkoxide in the presence of a hydrocarbon solvent, e.g. kerosine. The aluminium contaminants are removed by distillation or by washing with dilute acid, e.g. 2-40% aqueous sulphuric acid. Hydrogenation is then effected at 60-1000 DEG F., above 200 p.s.i.g., 0.5-6 vol/vol/hour with 600-5,000 SCF of hydrogen per barrel over any hydrogenation catalyst, e.g. nickel-molybdena on alumina, cobalt-molybdena on alumina, iron oxide, barium-copper chromite, molybdenum disulphide on alumina, or nickel sulphide on alumina. The product may be distilled and used as refinery distillates or reused as diluents in organoaluminium chemistry.

Production of substituted aromatic compounds

The alkylation of an aromatic hydrocarbon with a polymerizable organic compound is effected in the presence of a catalyst obtained by treating a halogenatable inorganic oxide with a halogenated organic compound. The oxide may be of a metal of Group IVa, Va or VIa, preferably titanium, alone or mixed with a minor proportion of alumina and is preferably calcined at 200-1100 DEG F. before being treated with a methane derivative, e.g. methylene dichloride, chloroform, carbon tetrachloride and the corresponding fluorine compounds. The amount of halogen added to the oxide may be 1-15%. The polymerizable compound may be olefinic, polyolefinic or acetylenic, particularly ethylene, propylene, butene-1 and 4-methyl-pentene-1 and the aromatic hydrocarbon may be benzene, toluene or a xylene. Reaction is effected at 20-200 DEG C. and any pressure. The product also contains some polymer from the polymerizable compound.

Catalyst for selective hydrogenation of acetylene

Catalysts for the selective hydrogenation of acetylene consist of an inert support material, palladium and silver in quantities of up to 5% by weight in respect of the entire quantity of catalyst, the properties of Pd being 99-60% by weight in respect of the total quantity of the two noble metals, and having an additional content of iron oxide amounting in weight to 20-80 times the total quantity of Pd and Ag. Specified as inert support is a -Al2O3. In examples a -Al2O3 is impregnated with nitrates of Fe, Pd and Ag in appropriate quantities followed by heat treatment to produce Fe2O3, Pd and Ag respectively. In Example 2, 77 parts of C2H4, 22 parts of C2H6, 1,15 parts of C2H2 are mixed with 2,3% by volume of H2 and after passage over a catalyst composition as above at 130 DEG C. less than 0,001% of C2H2 was present.

PROCESS FOR THE CATALYTIC SYNTHESIS OF HYDROCARBONS PARTICULARLY METHANE FROM HYDROGEN AND CARBON MONOXIDE

Improvements in or relating to catalytic isomerization processes

Hydrocarbons are isomerized at 200-400 DEG F. by contact with hydrogen in the presence of a catalyst comprising Pt and Al2O3 activated by contacting a composite of Pt and Al2O3 with an organic acid chloride having an atomic ratio of Cl: C of at least 2: 1 at an activation temperature of 300-650 DEG F. Suitable conditions include a space velocity of 0.5-2 vol/vol/hour and a hydrogen to hydrocarbon mol. ratio of 0.2-5: 1 using liquid or vapour phase at 300-500 p.s.i.g. Comparative examples refer to the isomerization of a hexane feedstock to yield 2-methyl pentane, 3-methyl pentane, 2: 2 dimethylbutane, 2: 3 dimethylbutane cyclic hydrocarbons and pentanes.ALSO:An isomerization catalyst comprises Al2O3 preferably eta alumina, 0,01-1,0% of Pt and 1,0-10% of chlorine, in which at least part of the chlorine is introduced at 300-650 DEG F. into the catalyst by use of an organic acid chloride having an atomic ratio of chlorine to carbon of at least 2 : 1. The catalyst may be used as a granular or ...

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 ...

Production of olefins

Hydrogenation of oligomers

Paraffins are prepared by hydrogenating olefinic oligomers of propylene and/or butylenes having 6 to 16 C atoms in the trickle phase in a practically stationary H2 atmosphere under 10-100 atmospheres pressure and at 80-250 DEG C. in the presence of platinum and/or palladium metal deposited on a carrier which contains no free inorganic acid or acid salt thereof. Specified catalyst carriers are alumina and calcium carbonate. The hydrogenation is preferably carried out in a tube reactor. In examples diisobutene, tri-isobutylene and tetra-isobutene are hydrogenated.

PROCESS FOR RE-ACTIVATION OF SOLID ACID CATALYST

PROCESS FOR THE CATALYTIC ISOMERIZATION OF TETRAHYDRODIMETHYLDICYCLOPENTADIENE

PREPARATION OF DIMETHYLNAPHTHALENES

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.

Process for preparing aromatics from methane

The present invention relates to a process for carrying out endothermic, heterogeneously catalyzed reactions in which the reaction of the starting materials is carried out in the presence of a mixture of inert heat transfer particles and catalyst particles, where the catalyst particles are regenerated in a nonoxidative atmosphere at regular intervals and the heat of reaction required is introduced by separating off the inert heat transfer particles, heating the heat transfer particles in a heating zone and recirculating the heated heat transfer particles to the reaction zone. The process of the invention is particularly suitable for the nonoxidative dehydroaromatization of C 1 -C 4 -aliphatics in the presence of zeolite-comprising catalysts.

Process for selectively making olefins from energy dense alcohols

A process to perform selective catalytic oxidation of four-carbon alcohols to produce four-carbon olefins with yields greater than 90%. The process includes providing a supply of oxygen gas and a butanol fuel, atomizing and evaporating the fuel to produce a vapor, mixing the vapor with the oxygen to form a fuel mixture, reacting the fuel mixture in the presence of a heated solid Rh/Al 2 O 3 or Al 2 O 3 catalysts.

Multiple zeolite catalyst

The multiple zeolite catalyst is a catalytic composition used to convert C 9+ alkylaromatic hydrocarbons to BTX, particularly commercially valuable xylenes. The catalyst is formed by mixing at least two zeolites selected from mordenite, beta zeolite, ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, MFI topology zeolite, NES topology zeolite, EU-1, MAPO-36, SAPO-5, SAPO-11, SAPO-34, and SAPO-41, and adding at least one metal component selected from Group VIB and Group VIII of the Periodic Table of the Elements. The two zeolites should have different physical and chemical characteristics, such as pore size and acidity. An exemplary catalyst includes mordenite, ZSM-5, and 3 wt. % molybdenum. The transalkylation reaction may be conducted in one or more reactors with a fixed bed, moving bed, or radial flow reactor at 200-540° C., a pressure of 1.0-5.0 MPa, and liquid hourly space velocity of 1.0-5.0 per hour.

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 producing fuels and solvents

Described herein are methods for producing fuels and solvents from fatty acid resources. Also disclosed herein are fuels and solvents produced by the methods described herein.

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.

Process For Producing Cyclohexylbenzene

In a process for producing cyclohexylbenzene, benzene and hydrogen are contacted under hydroalkylation conditions with a catalyst system comprising a MCM-22 family molecular sieve and at least one hydrogenation metal. The conditions comprise a temperature of about 140° C. to about 175° C., a pressure of about 135 psig to about 175 psig (931 kPag to 1207 kPag), a hydrogen to benzene molar ratio of about 0.30 to about 0.65 and a weight hourly space velocity of benzene of about 0.26 to about 1.05 hr −1 .

Process for the conversion of mixed lower alkanes to aromatic hydrocarbons

A process for the conversion of mixed lower alkanes into aromatics which comprises first reacting a mixed lower alkane feed comprising at least propane and ethane in the presence of an aromatization catalyst under reaction conditions which maximize the conversion of propane into first stage aromatic reaction products, separating ethane from the first stage aromatic reaction products, reacting ethane in the presence of an aromatization catalyst under reaction conditions which maximize the conversion of ethane into second stage aromatic reaction products, and optionally separating ethane from the second stage aromatic reaction products.

Production of lower olefins from synthesis gas

Disclosed is a process for the production of lower olefins by the conversion of a feed stream comprising carbon monoxide and hydrogen, and catalysts as used therein, such as a Fischer-Tropsch process. By virtue of the invention, lower olefins can be formed from synthesis gas, with high selectivity, and low production of methane. The catalysts used herein comprise an α-alumina support, and a catalytically active component that comprises iron-containing particles dispersed onto the support in at least 1 wt. %. The majority of the iron-containing particles is in direct contact with the α-alumina and is well-distributed thereon. Preferably, the iron-containing particles have an average particle size below 30 nm, and most preferably below 10 nm. The supported catalysts not only show a high selectivity, but also a high catalyst activity and chemical and mechanical stability.

Process for the dehydration of aqueous bio-derived terminal alcohols to terminal alkenes

A method and apparatus for dehydrating bio-1-alcohols to bio-l-alkenes with high selectivity. The bio-1-alkenes are useful in preparing high flashpoint diesel and jet biofuels which are useful to civilian and military applications. Furthermore, the bio-1-alkenes may be converted to biolubricants useful in the transporation sector and other areas requiring high purity/thermally stable lubricants.

Process for the regeneration of hydrocarbon conversion catalysts

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

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.

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.

Hydroisomerization and selective hydrogenation of feedstock in ionic liquid-catalyzed alkylation

A process for producing alkylate comprising contacting a first hydrocarbon stream comprising at least one olefin having from 2 to 6 carbon atoms which contains 1,3-butadiene and 1-butene with a hydroisomerization catalyst in the presence of hydrogen under conditions favoring the simultaneous selective hydrogenation of 1,3-butadiene to butenes and the isomerization of 1-butene to 2-butene and contacting the resulting stream and a second hydrocarbon stream comprising at least one isoparaffin having from 3 to 6 carbon atoms with an acidic ionic liquid catalyst under alkylation conditions to produce an alkylate is disclosed.

Production of renewable aromatic compounds

The invention provides a process for producing a variety renewable aromatic compounds such as benzene, toluene, xylenes, and cumene, as well as compounds derived from these including, for example, aniline, benzoic acid, cresol, cyclohexane, cyclohexanone, phenol and bisphenol A, toluene di-isocyanate, isophthalic acid, phthalic anhydride, terephthalic acid and dimethyl terephthalate. The invention also provides for renewable forms of these aromatic compounds.

Fischer-tropsch catalyst regeneration

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

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.

Nickel-M-Alumina Xerogel Catalyst, Method for Preparing the Same, and Method for Preparing Methane Using the Catalyst

A nickel-M-alumina hybrid xerogel catalyst for preparing methane, wherein the metal M is at least one element selected from the group consisting of Fe, Co, Ni, Ce, La, Mo, Cs, Y, and Mg, a method for preparing the catalyst and a method for preparing methane using the catalyst are provided. The catalyst has strong resistance against a high-temperature sintering reaction and deposition of carbon species, and can effectively improve a conversion ratio of carbon monoxide and selectivity to methane.

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.

Even carbon number paraffin composition and method of manufacturing same

Paraffin compositions including mainly even carbon number paraffins, and a method for manufacturing the same, is disclosed herein. In one embodiment, the method involves contacting naturally occurring fatty acid/glycerides with hydrogen in a slurry bubble column reactor containing bimetallic catalysts with equivalent particle diameters from about 10 to about 400 micron. The even carbon number compositions are particularly useful as phase change material.

ALUMINA MATERIALS WITH INCREASED SURFACE ACIDITY, METHODS FOR MAKING, AND METHODS FOR USING THE SAME

Aluminas with increased surface acidity, methods of making the same, and methods for using the same are provided. In an exemplary embodiment, a method for increasing the surface acidity of an alumina material includes providing an alumina starting material, and processing the alumina starting material under hydrothermal conditions in the presence of one or more organic acids to generate a hydrothermally treated alumina. In this embodiment, the one or more organic acids includes a polyprotic organic acid with a pKa value of about 0 to about 10, and the resulting hydrothermally treated alumina has increased surface acidity relative to the alumina starting material. 1. A method for increasing surface acidity of an alumina material , the method comprising the steps of:providing an alumina starting material; andprocessing the alumina starting material under hydrothermal conditions in the presence of an organic acid to generate a hydrothermally treated alumina,wherein the organic acid comprises a polyprotic organic acid with a pKa value of about 0 to about 10, and the hydrothermally treated alumina has increased surface acidity relative to the alumina starting material.2. The method of claim 1 , wherein the organic acids comprises tartaric acid claim 1 , malic acid claim 1 , citric acid claim 1 , or a mixture thereof.3. The method of claim 1 , wherein the alumina starting material comprises a gamma alumina.4. The method of claim 1 , wherein the hydrothermally treated alumina comprises a boehmite alumina.5. The method of claim 4 , further comprising calcining the hydrothermally treated alumina to convert at least a portion of the boehmite alumina in the hydrothermally treated alumina into a gamma alumina.6. The method of claim 5 , wherein the gamma alumina has a Brunauer claim 5 , Emmett and Teller (BET) surface area that is ±25% of the alumina starting material.7. The method of claim 4 , wherein substantially all of the hydrothermally treated alumina is a boehmite alumina ...

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.

Method For Producing Hydrocarbon Dehydrogenation Catalyst Using Sponge-Type Support

Disclosed are a catalyst for dehydrogenating a paraffinic hydrocarbon and a method of preparing the same, wherein the catalyst is configured such that a sponge-type alumina support having 3D meso/macro pores is directly impregnated with an active metal, thus decreasing the diffusion resistance of a material, realizing structural stability, and maximizing the distribution of the active metal in the support, thereby significantly increasing olefin conversion and selectivity. 1. A method of preparing a catalyst for dehydrogenating paraffin , comprising:providing a sponge-type alumina support having meso/macro pore sizes;thermally treating the support at 800 to 1200° C. for 2 to 10 hr in an air atmosphere;dispersing an active metal precursor in the support so as to be loaded into the support;drying the support having the loaded active metal at 80 to 150° C.; andfiring the dried catalyst at 500 to 900° C. for 2 to 10 hr in an air atmosphere.2. The method of claim 1 , further comprising reducing the fired catalyst at 400 to 700° C. in a hydrogen atmosphere claim 1 , after the firing the dried catalyst.3. The method of claim 1 , wherein the active metal comprises platinum claim 1 , tin claim 1 , or an alkali metal or alkaline earth metal.4. The method of claim 1 , wherein the sponge-type alumina support comprises two kinds of pores having a meso pore size and a macro pore size.5. The method of claim 1 , wherein the sponge-type alumina support is selected from the group consisting of alpha alumina claim 1 , theta alumina claim 1 , silicon carbide claim 1 , and mixtures thereof.6. The method of claim 1 , wherein the sponge-type alumina support has a specific surface area of 50 to 100 m/g claim 1 , a total pore volume of 0.1 to 0.7 cm/g claim 1 , and a pore size of 10 to 100 nm.7. A catalyst for dehydrogenating paraffin claim 1 , prepared by the method of any one of to .8. A method of producing an olefin claim 7 , comprising dehydrogenating a gas mixture comprising paraffin ...

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 , ...

METHOD OF PRODUCING A FUEL ADDITIVE

A method of producing a fuel additive includes producing a first product stream comprising butadiene by passing a feed stream comprising C4 hydrocarbons through a steam cracker; transforming greater than or equal to 90 weight % of the butadiene in the first product stream into a second product stream by passing the first product stream through a first hydrogenation unit, wherein the second product stream comprises 1-butene, 2-butene, n-butane, isobutylene, isobutane, or a combination thereof; and converting the second product stream into the fuel additive by passing the second product stream through a fuel additive synthesis unit with an acid catalyst. 1. A method of producing a fuel additive , comprising:producing a first product stream comprising butadiene by passing a feed stream comprising C4 hydrocarbons through a steam cracker;transforming greater than or equal to 90 weight % of the butadiene in the first product stream into a second product stream by passing the first product stream through a first hydrogenation unit, wherein the second product stream comprises 1-butene, 2-butene, n-butane, isobutylene, isobutane, or a combination thereof; andconverting the second product stream into the fuel additive by passing the second product stream through a fuel additive synthesis unit with an acid catalyst.2. The method of claim 1 , wherein the feed stream comprises a portion of an effluent from a fluid catalytic cracking process.3. The method of claim 1 , wherein the feed stream comprises at least one of methyl acetylene claim 1 , propylene claim 1 , 1 claim 1 ,3-butadiene claim 1 , 1 claim 1 ,2-butadiene claim 1 , isobutylene claim 1 , cis-2-butene claim 1 , trans-2-butene claim 1 , 1-butene claim 1 , propene claim 1 , isobutane claim 1 , or n-butane.4. The method of claim 1 , wherein greater than or equal to 95 weight % of the butadiene in the first product stream is transformed into the second product stream.5. The method of claim 1 , wherein the acid catalyst ...

GAS CLEAN-UP FOR ALKANE OXIDATIVE DEHYDROGENATION EFFLUENT

The invention relates to a process for the production of an alkene by alkane oxidative dehydrogenation, comprising: (a) subjecting a stream comprising an alkane to oxidative dehydrogenation conditions, comprising contacting the alkane with oxygen in the presence of a catalyst comprising a mixed metal oxide, resulting in a stream comprising alkene, unconverted alkane, water, carbon dioxide, unconverted oxygen, carbon monoxide and optionally an alkyne; (b) removing water from at least part of the stream comprising alkene, unconverted alkane, water, carbon dioxide, unconverted oxygen, carbon monoxide and optionally an alkyne resulting from step (a), resulting in a stream comprising alkene, unconverted alkane, carbon dioxide, unconverted oxygen, carbon monoxide and optionally alkyne; (c) removing unconverted oxygen, carbon monoxide and optionally alkyne from at least part of the stream comprising alkene, unconverted alkane, carbon dioxide, unconverted oxygen, carbon monoxide and optionally alkyne resulting from step (b), wherein carbon monoxide and optionally alkyne are oxidized into carbon dioxide, resulting in a stream comprising alkene, unconverted alkane and carbon dioxide; (d) optionally removing carbon dioxide from at least part of the stream comprising alkene, unconverted alkane in and carbon dioxide resulting from step (c), resulting in a stream comprising alkene and unconverted alkane; (e) optionally separating at least part of the stream comprising alkene and unconverted alkane resulting from step (d), into a stream comprising alkene and a stream comprising unconverted alkane; (f) optionally recycling unconverted alkane from at least part of the stream comprising unconverted alkane resulting from step (e), to step (a). 1. A process for the production of an alkene by alkane oxidative dehydrogenation , comprising:(a) subjecting a stream comprising an alkane to oxidative dehydrogenation conditions, comprising contacting the alkane with oxygen in the presence of a ...

Systems and Methods for Producing Naphthalenes and Methylnaphthalenes

A process for producing naphthalene or methylnaphthalenes from an alkane-containing stream. In an embodiment, the produce includes providing an alkane-containing feed stream to a reactor, and contacting the ethane-containing stream with an aromatization catalyst within the reactor. The aromatization catalyst comprises molecular sieve, and a dehydrogenation component. In addition, the process includes producing a reactor effluent stream from the reactor, and separating a product stream from the reactor effluent stream. The product stream comprises at least one or both of naphthalene and methylnaphthalene. 1. A process , comprising:(a) providing an alkane-containing feed stream to a reactor;(b) contacting the alkane-containing stream with an aromatization catalyst within the reactor, wherein the aromatization catalyst comprises molecular sieve, and a dehydrogenation component;(c) producing a reactor effluent stream from the reactor; and(d) separating a product stream from the reactor effluent stream, wherein the product stream comprises at least one or both of naphthalene and methylnaphthalene.2. The process of claim 1 , wherein the alkane-containing feed comprises a majority fraction of ethane.3. The process of claim 2 , wherein the molecular sieve of the aromatization catalyst comprises ZSM-5.4. The process of claim 3 , wherein the dehydrogenation component comprises gallium.5. The process of claim 4 , further comprising:(e) removing a majority of one or both of sulfur or nitrogen in the feed stream before providing the feed stream to the reactor in (a).6. The process of claim 5 , wherein the reactor effluent stream contains one or both of:less than 5 ppm sulfur; andless than 5 ppm of nitrogen.7. The process of claim 6 , wherein the contacting in (b) is carried out with a temperature of about 500° C. to about 625° C. claim 6 , a pressure of about 207 kPaa (30 psia) to about 522 kPaa (80 psia) claim 6 , and a WHSV of about 0.1 hrto about 10 hr.8. The process of claim ...

NATURAL GAS LIQUID UPGRADING BY IONIC LIQUID CATALYZED ALKYLATION

We provide a process, comprising: 1. A process for making one or more middle distillate alkylate products , comprising:a. dehydrogenating a natural gas feedstock comprising saturated hydrocarbons in a dehydrogenation reactor to produce a mixture comprising one or more olefins and one or more unconverted paraffins;b. without further purification or modification other than mixing with an isoparaffin, sending the mixture to a single alkylation reactor that is not thermally coupled with the dehydrogenation reactor;c. alkylating the one or more olefins with the isoparaffin in the single alkylation reactor, using an ionic liquid catalyst, to produce the one or more alkylate products; andd. distilling the one or more alkylate products and collecting a bottoms distillation fraction that is a middle distillate blending component having a sulfur level of 50 wppm or less and a Bromine number less than 1.2. The process of claim 1 , wherein the natural gas feedstock comprises paraffins in the range of from C2 to C6 paraffins.3. The process of claim 1 , wherein the natural gas feedstock is one of a C2 claim 1 , a C3 claim 1 , a C4 claim 1 , a C5 claim 1 , or a C6 paraffin.4. The process of claim 1 , wherein the mixture comprises from 30 to 80 wt % of the one or more unconverted paraffins.5. The process of claim 1 , wherein the one or more alkylate products are selected from the group consisting of an alkylate gasoline claim 1 , an alkylate jet fuel claim 1 , an alkylate diesel fuel claim 1 , and mixtures thereof.6. The process of claim 1 , wherein the isoparaffin is isobutane claim 1 , isopentane claim 1 , an isohexane claim 1 , or a combination thereof.7. The process of claim 1 , wherein a molar ratio of the isoparaffin to the one or more olefins in the single alkylation reactor is from 4:1 to 12:1.8. The process of claim 1 , wherein a molar ratio of the isoparaffin to the one or more olefins in the single alkylation reactor is adjusted to change a boiling range of the one or ...

PROCESS TO PREPARE PROPYLENE

The invention is directed to a process to prepare propylene from a mixture of hydrocarbons by performing the following steps. (a) extracting aromatics from the mixture of hydrocarbons thereby obtaining a mixture of hydrocarbons poor in aromatics, (b) contacting the mixture obtained in step (a) with a heterogeneous cracking catalyst as present in a fixed bed thereby obtaining a cracked effluent, (c) separating propylene from the cracked effluent thereby also obtaining a higher boiling fraction, (d) recycling part of the higher boiling fraction to step (b) and at least 5 wt % of the higher boiling fraction to step (a). () 1. A process to prepare propylene from a mixture of hydrocarbons by performing the following steps:a. extracting aromatics from the mixture of hydrocarbons thereby obtaining a mixture of hydrocarbons poor in aromatics,b. contacting the mixture obtained in step (a) with a heterogeneous cracking catalyst as present in a fixed bed thereby obtaining a cracked effluent,c. separating propylene from the cracked effluent thereby also obtaining a higher boiling fraction,d. recycling part of the higher boiling fraction to step (b) and at least 5 wt % of the higher boiling fraction to step (a).2. The process according to claim 1 , wherein in step (d) between 10 and 30 wt % of the higher boiling fraction is recycled to step (a).3. The process according to claim 1 , wherein the mixture of hydrocarbons comprises any one of:(a) between 1 and 70 wt % olefins having 4 or more carbon atoms; or(b) between 1 and 20 wt % olefins having 4 or more carbon; or(c) a mixture of paraffins, olefins, naphthenic and aromatic compounds boiling for more than 90 wt % between 35 and 250° C.4. (canceled)5. (canceled)6. The process according to claim 3 , wherein the mixture of hydrocarbons comprises any one or more of: a light straight run naphtha claim 3 , a fraction as isolated from the effluent selected from of any one or more of the following processes: Fluid Catalytic Cracking ...

DEHYDROGENATION CATALYSTS AND METHODS FOR USING THEM

The present disclosure relates to gallium-based dehydrogenation catalysts that further include additional metal components, and to methods for dehydrogenating hydrocarbons using such catalysts. One aspect of the disclosure provides a calcined dehydrogenation catalyst that includes a gallium species, a cerium species, a platinum promoter, and a silica-alumina support. Optionally, the composition can include a promoter selected from the alkali metals and alkaline earth metals. 1. A dehydrogenation catalyst composition comprisingGa, present in the composition in an amount within the range of 0.5 wt. % to 20 wt. %, calculated as elemental metal on a calcined basis;Ce, present in the composition in an amount within the range of 0.2 wt. % to 20 wt. %, calculated as elemental metal on a calcined basis;Pt, present in the composition in an amount within the range of 1 ppm to 500 ppm, calculated as elemental metal on a calcined basis;optionally, a promoter M2 selected from the alkali metals, the alkaline earth metals, and any mixture thereof, present in the composition in an amount of up to 20 wt. %, calculated as elemental metal on a calcined basis; and{'sub': '2', 'a silica-alumina support S1, present in the composition in an amount within the range of 50 wt. % to 99 wt. %, calculated as oxide on a calcined basis, silica being present in S1 in an amount within the range of 1 wt. % to 30 wt. %, calculated as SiOon a calcined basis.'}2. The catalyst composition of claim 1 , wherein Ga is present in the composition in an amount within the range of 1.5 wt. % to 10 wt. % claim 1 , e.g. claim 1 , 1.5 wt. % to 8.5 wt. % claim 1 , or 1.5 wt. % to 7 wt. % claim 1 , or 1.5 wt. % to 5 wt. % claim 1 , or 1.5 wt. % to 3 wt. % claim 1 , calculated as elemental metal on a calcined basis.3. The catalyst composition of claim 1 , wherein Ce is present in the composition in an amount of 0.5 wt. % to 20 wt. % claim 1 , e.g. claim 1 , 0.5 wt. % to 15 wt. % claim 1 , or 0.5 wt. % to 10 wt. % ...

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 ...

FLUIDIZABLE CATALYSTS FOR OXIDATIVE DEHYDROGENATION OF HYDROCARBONS

Fluidizable catalysts for oxygen-free oxidative dehydrogenation of alkanes to corresponding olefins. The catalysts contain 10-20% (by weight per total catalyst weight) of one or more vanadium oxides as the catalytic material, which are mounted upon an alumina support that is modified with zirconia at alumina/zirconia ratios of 5:1 up to 1:2. Various methods of preparing and characterizing the fluidizable catalysts are also provided. 1: A fluidizable catalyst for oxidative dehydrogenation of an alkane comprising:a zirconia-modified alumina support material; and10-20% of one or more vanadium oxides by weight based on the total catalyst weight, the one or more vanadium oxides being adsorbed onto the support material;wherein the support material comprises an alumina/zirconia weight ratio of 1-5:1-3.2: The fluidizable catalyst of claim 1 , wherein the one or more vanadium oxides are selected from the group consisting of VO claim 1 , VOand VO.3: The fluidizable catalyst of claim 2 , comprising at least 50% of VObased on total weight of the one or more vanadium oxides.4: The fluidizable catalyst of claim 1 , wherein the alumina/zirconia weight ratio is 1-2:1.5: The fluidizable catalyst of claim 1 , wherein the one or more vanadium oxides form a crystalline phase on the surface of the zirconia-modified alumina support material.6: The fluidizable catalyst of claim 1 , having an average particle size of 40-120 μm.7: The fluidizable catalyst of claim 1 , wherein the fluidizable catalyst comprises a plurality of particles and more than 75% of the particles are in the 40-120 μm size range.8: The fluidizable catalyst of claim 1 , having an apparent particle density of 1.5-3.5 g/cm.9: The fluidizable catalyst of claim 1 , having Class B powder properties in accordance with Geldart particle classification.10: The fluidizable catalyst of claim 1 , having a BET surface area of 10-50 m/g.11: The fluidizable catalyst of claim 1 , wherein the zirconia present in the alumina/zirconia ...

METHOD FOR PREPARING HIGHLY NITROGEN-DOPED MESOPOROUS CARBON COMPOSITES

Some embodiments are directed to a new methodology aimed at preparing highly N-doped mesoporous carbon macroscopic composites, and their use as highly efficient heterogeneous metal-free catalysts in a number of industrially relevant catalytic transformations. 1. A method of preparing macroscopic composites made of a macroscopic support coated with a thin layer of highly nitrogen-doped mesoporous carbon phase (active phase) , said method comprising:{'sub': 4', '2', '3, '(a) providing an aqueous solution of (i) (NH)CO; (ii) a carbohydrate as carbon source, selected from aldose monosaccharides and glycosilated forms thereof, disaccharides and oligosaccharides or dextrine deriving from biomass conversion, and (iii) a carboxylic acid source selected from citric acid, and any other mono-, di-, tri-, and poly-carboxylic acid or their ammonium mono-, di-, tri- and poly-basic forms;'} [ (a1) providing an aqueous solution of citric acid and a carbohydrate as carbon source, selected from aldose monosaccharides and glycosilated forms thereof, disaccharides and oligosaccharides;', '(c1) prior to step (c), immerging/soaking or impregnating the macroscopic support of step (b) in the aqueous solution of step (a1) for a suitable amount of time;', '(d1) optionally removing the immerged macroscopic support from the aqueous solution of step (a1) if an excess aqueous solution is used in step (c1);', '(e1′) optionally subjecting the resulting macroscopic support to a gentle thermal treatment (drying) under air at low temperatures from 45 to 55° C., preferably 50° C.±3° C.;', '(e1) subjecting the resulting macroscopic support to a first thermal treatment (drying) under air at moderate temperatures from 110-150° C.±5° C., preferably 130° C.±5° C.; and', '(f1) subjecting the thermally treated (dried) macroscopic support to a second thermal treatment under inert atmosphere at higher temperatures from 600-800° C.±10° C., preferably 600° C.±5° C.; thereby generating a macroscopic composite ...

PROCESS FOR MAKING LINEAR LONG-CHAIN ALKANES FROM RENEWABLE FEEDSTOCKS USING CATALYSTS COMPRISING HETEROPOLYACIDS

A hydrodeoxygenation process for producing a linear alkane from a feedstock comprising a saturated or unsaturated Coxygenate that comprises an ester group, carboxylic acid group, carbonyl group and/or alcohol group is disclosed. This process comprises contacting the feedstock with (i) a catalyst comprising about 0.1% to about 10% by weight of a metal selected from Group IB, VIB, or VIII of the Periodic Table, and (ii) a heteropolyacid or heteropolyacid salt, at a temperature between about 150° C. to about 250° C. and a hydrogen gas pressure of at least about 300 psig. By contacting the feedstock with the catalyst and heteropolyacid or heteropolyacid salt under these temperature and pressure conditions, the Coxygenate is hydrodeoxygenated to a linear alkane that has the same carbon chain length as the Coxygenate. 1. A hydrodeoxygenation process for producing a linear alkane from a feedstock comprising a saturated or unsaturated Coxygenate comprising a moiety selected from the group consisting of an ester group , carboxylic acid group , carbonyl group , and alcohol group , wherein the process comprises:{'sub': 10-18', '10-18, 'a) contacting said feedstock with (i) a catalyst comprising about 0.1% to about 10% by weight of a metal selected from Group IB, VIB, or VIII of the Periodic Table, and (ii) a heteropolyacid or heteropolyacid salt, at a temperature between about 150° C. to about 250° C. and a hydrogen gas pressure of at least about 300 psig, wherein the Coxygenate is hydrodeoxygenated to a linear alkane, and wherein the linear alkane has the same carbon chain length as the Coxygenate; and'}b) optionally, recovering the linear alkane produced in step (a).2. The hydrodeoxygenation process of claim 1 , wherein said Coxygenate is a fatty acid or a triglyceride.3. The hydrodeoxygenation process of claim 1 , wherein said feedstock comprises a plant oil or a fatty acid distillate thereof.4. The hydrodeoxygenation process of claim 3 , wherein said feedstock comprises(i) ...

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 outer portion of a given catalyst particle is Couter, the average concentration of the hydrogenation metal in the center portion of the given catalyst particle is Ccenter, where Crim/Ccenter≧2.0 and/or Couter/Ccenter2.0. Also disclosed are rimmed catalyst and process for making phenol and/or cyclohexanone using the catalyst. 1. A process for producing an alkylated aromatic compound , the process comprising 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 outer portion of a given catalyst particle is Couter; andthe average concentration of the hydrogenation metal in the center portion of the given catalyst particle is Ccenter; andat least one of the following conditions is met:(i) Crim/Ccenter≧2.0; and(ii) Couter/Ccenter≧2.0.2. The process of claim 1 , wherein the ...

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 ...

Linear Alpha Olefin Processes

The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes oligomerizing an olefin in the presence of a catalyst and a process solvent in at least one reactor, quenching the reactor effluent, and subjecting the quenched effluent to separation steps to obtain a stream enriched in one or more linear alpha olefins. 1. A method for forming one or more linear alpha olefins , the method comprising the steps of:(a) providing a feed comprising an olefin, a catalyst, and a process solvent to a reaction zone including at least one reactor under oligomerization conditions to obtain a reactor effluent produced in the at least one reactor;(b) contacting at least a portion of the reactor effluent with a quench agent to obtain a quenched effluent;(c) separating at least a portion of the quenched effluent to obtain a vapor effluent and a liquid effluent;(d) separating at least a portion of the liquid effluent to obtain at least one aqueous phase enriched in catalyst and quench agent and an organic phase depleted in catalyst and quench agent;(e) separating at least a portion of the organic phase to obtain a stream enriched in one or more linear alpha olefins.2. The process of claim 1 , wherein the feed comprises <25 ppb water by weight.3. The method of claim 1 , wherein step (a) comprises:providing the feed to a first tubular reactor under oligomerization conditions to obtain a first effluent; andtransferring the first effluent to a second tubular reactor under oligomerization conditions to obtain the reactor effluent.4. The method of claim 3 , further comprising providing steam to a first steam jacket disposed around the first tubular reactor and providing steam to a second team jacket disposed around the second tubular reactor claim 3 ,optionally further comprising controlling the pressure of steam in the first steam jacket pressure ...

Production Method for 1-Chloro-3,3,3-Trifluoropropene

A production method of 1-chloro-3,3,3-trifluoropropene according to the present invention includes reaction of 1,1,1,3,3-pentachloropropane with hydrogen fluoride, characterized in that the concentrations of respective catalytic components in the 1,1,1,3,3-pentachloropropane as the raw material is controlled to a predetermined level or less. By controlling the concentrations of the respective catalytic components in the 1,1,1,3,3-pentachloropropane to the predetermined level or less, it is possible to improve the problems of shortening of catalyst life, retardation of reaction and scaling or corrosion of equipment in the production of the 1-chloro-3,3,3-trifluoropropene. In addition, the 1,1,1,3,3-pentachloropropane can be obtained selectively with high yield by telomerization reaction of carbon tetrachloride and vinyl chloride. The present invention is thus useful as the method for industrially advantageous, high-yield production of the 1-chloro-3,3,3-trifluoropropene. 1. A method for producing 1-chloro-3 ,3 ,3-trifluoropropene , comprising reacting 1 ,1 ,1 ,3 ,3-pentachloropropane with hydrogen fluoride in a reaction system ,wherein the method comprises a concentration control step of controlling the concentrations of a metal solubilizer and/or a hydrochloride thereof and an iron complex in the 1,1,1,3,3-pentachloropropane supplied to the reaction system to be 100 ppm or less.2. The method according to claim 1 , wherein the metal solubilizer is at least one kind selected from the group consisting of N claim 1 ,N-dimethylacetamide claim 1 , acetonitrile claim 1 , 2-aminoacetonitrile claim 1 , N claim 1 ,N-dimethylformamide and hexamethylphosphoric amide.3. The method according to claim 1 , wherein the iron complex is a complex of N claim 1 ,N-dimethylacetamide claim 1 , iron (II) chloride and iron (III) chloride (FeCl.2FeCl.6DMAC).4. The method according to claim 1 , wherein the concentration control step includes claim 1 , before supplying the 1 claim 1 ,1 claim 1 ...

Catalyst for dehydration reaction of primary alcohols, method for preparing the same and method for preparing alpha-olefins using the same

Provided are a catalyst for dehydration reaction of a primary alcohol, a method for preparing the same, and a method for preparing alpha-olefins using the same. According to the present invention, there is provided a catalyst for dehydration reaction of primary alcohols capable of adjusting the strength and distribution of Lewis acid sites (LASs) on a surface of an alumina catalyst to realize high selectivity to alpha-olefins as well as a high conversion rate in the dehydration reaction of primary alcohols. Therefore, high-purity alpha-olefins having a low isomeric yield fraction as well as a high conversion rate can be produced from the primary alcohols.

METHODS AND SYSTEMS FOR ENERGY CONVERSION AND GENERATION

The invention relates to methods and systems of converting electrical energy to chemical energy and optionally reconverting it to produce electricity as required. In preferred embodiments the source of electrical energy is at least partially from renewable source. The present invention allows for convenient energy conversion and generation without the atmospheric release of CO2. One method for producing methane comprises electrolysis of water to form hydrogen and oxygen, and using the hydrogen to hydrogenate carbon dioxide to form methane. It preferred to use the heat produced in the hydrogenation reaction to heat the water prior to electrolysis. The preferred electrical energy source for the electrolysis is a renewable energy source such as solar, wind, tidal, wave, hydro or geothermal energy. The method allows to store the energy gained at times of low demand in the form of methane which can be stored and used to generate more energy during times of high energy demand. A system comprising an electrolysis apparatus and a hydrogenation apparatus, and a pipeline for the transportation of two fluids, is also described.

POROUS FORMED BODY AND PRODUCTION METHOD THEREOF, alpha-OLEFIN DIMERIZATION CATALYST AND PRODUCTION METHOD THEREOF, AND METHOD OF PRODUCING alpha-OLEFIN DIMER

A porous formed body (Y) including a porous formed body (X) that satisfies the following (x-1) to (x-3), and an alkali metal carbonate or an alkali metal bicarbonate, in which a content of the alkali metal carbonate or the alkali metal bicarbonate is in a range of from 1 part by mass to 230 parts by mass, with respect to 100 parts by mass of the porous formed body (X), and a production method thereof, an α-olefin dimerization catalyst and a production method thereof, and a method of producing an α-olefin dimer: 1. A porous formed body (Y) , comprising:a porous formed body (X) that satisfies the following requirements (x-1) to (x-3); andan alkali metal carbonate or an alkali metal bicarbonate,wherein a content of the alkali metal carbonate or the alkali metal bicarbonate is in a range of from 1 part by mass to 230 parts by mass, with respect to 100 parts by mass of the porous formed body (X):requirement (x-1): a volume of pores with a pore diameter in a range of from 0.01 μm to 100 μm is from 0.10 mL/g to 1.00 mL/g;requirement (x-2): a median pore diameter of pores with a pore diameter in a range of from 0.01 μm to 100 μm is from more than 0.01 μm to 10.0 μm; andrequirement (x-3): a crushing strength is from 0.7 kgf to 15.0 kgf.2. The porous formed body (Y) according to claim 1 , wherein the porous formed body (X) further satisfies the following requirement (x-4):requirement (x-4): the porous formed body (X) contains at least one compound selected from the group consisting of an oxide of a metal or a rare earth element and a complex oxide thereof, zeolite, activated carbon, and SiC.3. The porous formed body (Y) according to claim 1 , wherein the alkali metal carbonate or the alkali metal bicarbonate is at least one compound selected from the group consisting of NaCO claim 1 , NaHCO claim 1 , KCO claim 1 , and KHCO.4. The porous formed body (Y) according to claim 1 , wherein the porous formed body (Y) has a volume of pores with a pore diameter in a range of from 0.01 ...

Olefin aromatization catalyst, preparation method and use thereof, and low-carbon olefin aromatization process

The present discloses an aromatization catalyst, preparation process and application thereof and a low-carbon olefin aromatization process. The aromatization catalyst comprises a microporous material, a binder and a modifier; the microporous material is a zeolite molecular sieve, the binder is alumina, the modifier is phosphorus, and the molar ratio of the aluminum element in the binder to the phosphorus element is more than or equal to 1 and less than 5; the ratio of the acidity of the strongly acidic sites to the acidity of the weakly acidic sites of the olefin aromatization catalyst is less than 1.

Processes for Converting Aromatic Hydrocarbons via Alkyl-Demethylation

Alkyl-demethylation of C2+-hydrocarbyl substituted aromatic hydrocarbons can be utilized to treat one or more of a heavy naphtha reformate stream, a hydrotreated SCN stream, a C8 aromatic hydrocarbon isomerization feed stream, a C9+ aromatic hydrocarbon transalkylation feed stream, and similar hydrocarbon streams to produce additional quantity of xylene products. 1. A process for making xylenes , the process comprising:(I) providing a C6+ aromatic hydrocarbon-containing stream comprising a C2+-hydrocarbyl-substituted aromatic hydrocarbon, wherein the C2+-hydrocarbyl-substituted aromatic hydrocarbon has (i) a C2+ alkyl substitute attached to an aromatic ring therein and/or (ii) an aliphatic ring annelated to an aromatic ring therein;(II) optionally contacting the C6+ aromatic hydrocarbon-containing stream with a first alkyl-demethylation catalyst in a first alkyl-demethylation zone under a first set of alkyl-demethylation conditions to convert at least a portion of the C2+-hydrocarbyl-substituted aromatic hydrocarbon to an alkyl-demethylated aromatic hydrocarbon to obtain an optional first alkyl-demethylated effluent exiting the first alkyl-demethylation zone;(III) separating at least a portion of the C6+ aromatic hydrocarbon-containing stream and/or the first alkyl-demethylated effluent in a first separation apparatus to obtain a C6-C7 hydrocarbons-rich stream and a first C8+ aromatic hydrocarbons-rich stream;(IV) optionally contacting the first C8+ aromatic hydrocarbons-rich stream with a second alkyl-demethylation catalyst in a second alkyl-demethylation zone under a second set of alkyl-demethylation conditions to convert at least a portion of the C2+-hydrocarbyl-substituted aromatic hydrocarbon, if any, contained in the first C8+ aromatic hydrocarbons-rich stream to an alkyl-demethylated aromatic hydrocarbon to obtain an optional second alkyl-demethylated effluent exiting the second alkyl-demethylation zone;(V) separating at least a portion of the first C8+ ...

Transalkylation Processes for Converting Aromatic Hydrocarbons Comprising Alkyl-Demethylation

Alkyl-demethylation of C2+-hydrocarbyl substituted aromatic hydrocarbons can be utilized to treat one or more of a heavy naphtha reformate stream, a hydrotreated SCN stream, a C8 aromatic hydrocarbon isomerization feed stream, a C9+ aromatic hydrocarbon transalkylation feed stream, and similar hydrocarbon streams to produce additional quantity of xylene products.

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 ...

METHOD FOR DEHYDRATING A MIXTURE CONTAINING ETHANOL AND ISOPROPANOL

Production of a mixture of ethylene and propylene from a mixture containing ethanol and isopropanol and having a water content between 30 and 75 wt. % is obtained by a process comprising: 2. Process according to claim 1 , in which the mixture contains between 1 and 75% by weight of ethanol and between 99 and 25% by weight of isopropanol with respect to the total weight of ethanol and isopropanol.3. Process according to claim 1 , in which the aluminas (A) and (B) are gamma aluminas.4. Process according to claim 1 , in which the alumina (A) has a mean mesopore diameter comprised between 6 and 12 nm and preferably comprised between 7 and 11 nm.5. Process according to claim 1 , in which the alumina (B) has a BET specific surface area measured according to the standard ASTM D 3663-03 comprised between 150 and 180 m/g.6. Process according to claim 1 , in which the alumina (B) has a mean mesopore diameter comprised between 15 and 20 nm.7. Process according to claim 1 , in which when the mixture also comprises butanol claim 1 , said mixture is treated in order to separate the butanol before dehydration stage a).8. Process according to claim 7 , in which a separation of the butanol is carried out by distillation.930305343735. Process according to claim 1 , in which before stage a) the mixture is brought into contact with an aromatic cut comprising a mixture of aromatic compounds having 7 to 10 carbon atoms claim 1 , in a separation unit comprising a liquid-liquid extraction column () claim 1 , so as to separate from said extraction column () an aqueous fraction () and an organic fraction containing the aromatic cut claim 1 , ethanol and isopropanol claim 1 , and said organic fraction is sent into a distillation column () configured in order to extract an effluent () containing the aromatic cut and a mixture () containing ethanol and isopropanol claim 1 , and said mixture is sent into the dehydration unit.10. Process according to claim 9 , in which the aromatic cut is a ...

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.

MULTIMETALLIC CATALYSTS FOR METHANATION OF CARBON DIOXIDE AND DRY REFORMING OF METHANE

Processes for forming multimetallic catalysts by grafting nickel precusors to metal oxide supports. Dry reforming reaction catalysts having nickel and promotors grafted to metal oxides supports. Methanation reaction catalysts having nickel and promotors grafted to metal oxides supports. 1. A method of forming a multimetallic catalyst comprising:{'sub': 2', '3', '2', '2', '2, 'grafting an organometallic promotor comprising a metal selected from the group consisting of B, Cu, Co, Fe, Mn, Sn, Mg, V, and Zn and an organic ligand, onto a metal oxide support selected from the group consisting of AlO, CeO, MgO, SiO, and TiO, forming a promotor-support material;'}calcine the organometallic promotor in air to form a calcined promotor-support material;grafting an organonickel precursor grafted onto the calcined promotor-support material; andreducing the organonickel grafted promotor-support material to form an active multimetallic catalyst.2. The method of claim 1 , wherein reducing comprises reduction with 5-20% hydrogen at 200-600° C. for 2 hours and the active multimetallic catalyst is a methanation reaction catalyst.3. The method of claim 2 , wherein reducing comprises reduction with 10% hydrogen at 500° C. for 2 hours.4. The method of claim 2 , wherein the metal oxide support comprises CeO.5. The method of claim 4 , wherein the metal is selected from the group consisting of B claim 4 , Co claim 4 , Mn claim 4 , Sn claim 4 , and V.6. The method of claim 1 , wherein the wherein the oxide support comprises AlO.7. The method of claim 4 , wherein the metal is selected from the group consisting of Mg and V.8. The method of claim 1 , wherein reducing comprises reduction with 5-20% hydrogen at 700-850° C. for 2 hours and the active multimetallic catalyst is a dry reforming reaction catalyst.9. The method of claim 1 , wherein reducing comprises reduction with 10% hydrogen at 800° C. for 2 hrs.10. The method of claim 8 , wherein the wherein oxide support is selected from the group ...

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 FOR PRODUCING INDENE

The present invention provides a production method for indene, comprising a dehydrogenation step of obtaining a reaction product containing indene by contacting a raw material gas containing indane and molecular hydrogen with a dehydrogenation catalyst, wherein the dehydrogenation catalyst comprises a support containing aluminum, and a supported metal supported on the support, the supported metal contains a group 14 metal element and platinum, and an atomic ratio of the group 14 metal element to the platinum in the dehydrogenation catalyst is 8.0 or less. 1. A production method for indene , comprising a dehydrogenation step of obtaining a reaction product containing indene by contacting a raw material gas containing indane and molecular hydrogen with a dehydrogenation catalyst ,wherein the dehydrogenation catalyst comprises a support containing aluminum, and a supported metal supported on the support,the supported metal contains a group 14 metal element and platinum, andan atomic ratio of the group 14 metal element to the platinum in the dehydrogenation catalyst is 8.0 or less.2. The production method according to claim 1 , wherein the atomic ratio of the group 14 metal element to the platinum in the dehydrogenation catalyst is 3.5 or more and 7.0 or less.3. The production method according to claim 1 , wherein the group 14 metal element is tin.4. The production method according to claim 1 , wherein the group 14 metal element and the platinum are supported on the support by using a metal source not containing a chlorine atom.5. The production method according to claim 1 , wherein a molar ratio of the molecular hydrogen to the indane in the raw material gas is 3.5 or less.6. The production method according to claim 1 , further comprising a raw material synthesis step of obtaining indane by dehydrogenation reaction of tetrahydroindene. The present invention relates to a production method for indene.Indene is an industrially useful substance as a material of a coumarone ...

Catalyst System and Use in Heavy Aromatics Conversion Processes

Disclosed are a catalyst system and its use in a process for the conversion of a feedstock containing C 8 + aromatic hydrocarbons to produce light aromatic products, comprising benzene, toluene and xylene. The catalyst system comprises (a) a first catalyst bed comprising a first catalyst composition, said first catalyst composition comprising a zeolite having a constraint index of 3 to 12 combined (i) optionally with at least one first metal of Group 10 of the IUPAC Periodic Table, and (ii) optionally with at least one second metal of Group 11 to 15 of the IUPAC Periodic Table; and (b) a second catalyst bed comprising a second catalyst composition, said second catalyst composition comprising (i) a meso-mordenite zeolite, combined (ii) optionally with at least one first metal of Group 10 of the IUPAC Periodic Table, and (iii) optionally with at least one second metal of Group 11 to 15 of the IUPAC Periodic Table, wherein said meso-mordenite zeolite is synthesized from TEA or MTEA and having a mesopore surface area of greater than 30 m 2 /g and said meso-mordenite zeolite comprises agglomerates composed of primary crystallites, wherein said primary crystallites have an average primary crystal size as measured by TEM of less than 80 nm and an aspect ratio of less than 2.

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 ...

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 ...

ALUMINA HAVING ACIDITY AND STRUCTURE WITH A POROSITY WHICH ARE OPTIMAL

An alumina exhibiting a structure with a porosity such that the volume of the pores having a diameter of between 70 and 2000 Å is between 0.15 and 0.50 ml/g, and comprising at least one alkali metal (M), such that the content by weight of alkali metal, expressed as MO, is between 400 and 1500 ppm, with respect to the total weight of the alumina, and a process for the transformation of a feedstock comprising at least one alcohol into an olefinic effluent, said process comprising a stage of dehydration of said alcohol in the presence of the alumina according to the present invention, having an acidity and a structure with a porosity which are optimal. 1. Alumina exhibiting a structure with a porosity such that the volume of the pores having a diameter of between 70 and 2000 Å is between 0.15 and 0.50 ml/g , and comprising at least one alkali metal (M) , such that the content by weight of alkali metal , expressed as MO , is between 400 and 1500 ppm , with respect to the total weight of the alumina.2. Alumina according to claim 1 , in which the volume of the pores having a diameter of between 70 and 2000 Å is greater than or equal to 0.15 ml/g claim 1 , preferably greater than or equal to 0.20 ml/g claim 1 , and less than or equal to 0.50 ml/g claim 1 , preferably less than or equal to 0.40 ml/g.3. Alumine according to claim 1 , in which the content by weight of alkali metal claim 1 , expressed as MO claim 1 , is between 400 and 950 ppm claim 1 , with respect to the total weight of the alumina.4. Alumina according to claim 1 , in which the total pore volume is greater than or equal to 0.50 ml/g.5. Alumina according to claim 1 , exhibiting a volume of the pores with a diameter of greater than or equal to 70 Å claim 1 , denoted V claim 1 , of greater than or equal to 0.35 ml/g claim 1 , preferentially of greater than or equal to 0.45 ml/g claim 1 , in a preferred way of greater than or equal to 0.50 ml/g and more preferably still of greater than or equal to 0.52 ml/g.6. ...

CATALYSTS THAT INCLUDE IRON, COBALT, AND COPPER, AND METHODS FOR MAKING THE SAME

According to one or more embodiments presently disclosed, a catalyst for converting hydrocarbons may include catalytic oxidized metal materials comprising oxidized iron, oxidized cobalt, and oxidized copper. At least 95 wt. % of the catalytic oxidized metal materials may be a combination of oxidized iron, oxidized cobalt, and oxidized copper. The catalyst may additionally include a mesoporous support material comprising pores having an average pore diameter of from 2 nm to 50 nm. At least 95 wt. % of the mesoporous support material may comprise alumina. At least 95 wt. % of the catalyst may be the combination of the catalytic oxidized metal materials and the mesoporous support material. Additional embodiments are included, such as methods for making the presently disclosed catalysts. 1. A catalyst for converting hydrocarbons , the catalyst comprising:catalytic oxidized metal materials comprising oxidized iron, oxidized cobalt, and oxidized copper, where at least 95 wt. % of the catalytic oxidized metal materials are a combination of the oxidized iron, the oxidized cobalt, and the oxidized copper; anda mesoporous support material comprising pores having an average pore diameter of from 2 nm to 50 nm, where at least 95 wt. % of the mesoporous support material comprises alumina; andwhere at least 95 wt. % of the catalyst is the combination of the catalytic oxidized metal materials and the mesoporous support material.2. The catalyst of claim 1 , where the weight ratio of iron atoms:cobalt atoms:copper atoms in the catalyst is 1:0.4-0.6:0.5-0.7.3. The catalyst of claim 1 , where the mesoporous support material comprises alumina material or silica material.4. The catalyst of claim 3 , where the mesoporous support material comprises gamma alumina.5. The catalyst of claim 1 , where the mesoporous support material comprises a hierarchical structured material comprising a silicate or aluminosilicate.6. The catalyst of claim 5 , where the hierarchical structured material is ...

OLEFIN OLIGOMERIZATIONS USING CHEMICALLY-TREATED SOLID OXIDES

Disclosed is a polyalphaolefin made up of hydrogenated oligomers. The oligomers include at least 80 wt. % of a Cto Cnormal alpha olefin monomer. The polyalphaolefin has a viscosity index greater than or equal to 110 and a kinematic viscosity at −40° C. of less than or equal to 1750 cSt. 1. A polyalphaolefin consisting essentially of hydrogenated oligomers , the oligomers comprising at least 80 wt. % of a Cto Cnormal alpha olefin monomer , wherein the polyalphaolefin has a viscosity index greater than or equal to 110 and a kinematic viscosity at −40° C. of less than or equal to 1750 cSt.216. The polyalphaolefin of claim , wherein the oligomers comprise at least 92.5 wt. % of a Cto Cnormal alpha olefin monomer.316. The polyalphaolefin of claim , wherein:the viscosity index is in a range from 110 to 125; andthe kinematic viscosity at −40° C. is in a range from 1300 to 1700 cSt.416. The polyalphaolefin of claim , wherein the polyalphaolefin has a kinematic viscosity at 40° C. in a range from 9 to 15 cSt.516. The polyalphaolefin of claim , wherein the polyalphaolefin has a kinematic viscosity at 100° C. in a range from 1.8 to 12 cSt.6. The polyalphaolefin of claim 1 , wherein:the viscosity index is in a range from 110 to 150; andthe kinematic viscosity at −40° C. is in a range from 1200 to 1750 cSt.7. The polyalphaolefin of claim 6 , wherein the polyalphaolefin has a kinematic viscosity at 40° C. in a range from 9 to 18 cSt.8. The polyalphaolefin of claim 6 , wherein the polyalphaolefin has a kinematic viscosity at 100° C. in a range from 1.8 to 10.4 cSt.9. The polyalphaolefin of claim 6 , wherein the viscosity index is in a range from 112 to 150.10. A process comprising:{'sub': 12', '16, '(i) introducing a monomer comprising a Cto Colefin and a chemically-treated solid oxide into a reaction zone, the chemically-treated solid oxide comprising sulfated alumina; and'}(ii) oligomerizing the monomer to form an oligomer product in the reaction zone.11. The process of claim 10 ...

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 THE HYDROGENATION OF AROMATICS USING A NICKEL-BASED CATALYST

Hydrogenation of at least one aromatic or polyaromatic compound contained in a hydrocarbon feedstock having a final boiling point below or equal to 650° C., at a temperature of between 30 and 350° C., at a pressure of between 0.1 and 20 MPa, at a hydrogen/(aromatic compounds to be hydrogenated) molar ratio between 0.1 and 10 and at an hourly space velocity HSV of between 0.05 and 50 h, in the presence of a catalyst comprising an alumina support and an active phase comprising nickel, prepared by 1. A process for the hydrogenation of at least one aromatic or polyaromatic compound contained in a hydrocarbon feedstock having a final boiling point below or equal to 650° C. , said process being carried out in the gas phase or in the liquid phase , at a temperature of between 30 and 350° C. , at a pressure of between 0.1 and 20 MPa , at a hydrogen/(aromatic compounds to be hydrogenated) molar ratio between 0.1 and 10 and at an hourly space velocity HSV of between 0.05 and 50 h , in the presence of a catalyst comprising an alumina support and an active phase comprising nickel , said active phase not comprising a metal from Group VIB , said catalyst being prepared by a process comprising at least:i) a step of bringing said support into contact with at least one solution containing at least one nickel precursor,ii) a step of bringing said support into contact with at least one solution containing at least one organic compound comprising at least one carboxylic acid function, or at least one alcohol function, or at least one ester function, or at least one amide function; 'steps i) and ii) being carried out separately, in any order, or at the same time.', 'iii) a step of drying said impregnated support at a temperature below 250° C.;'}2. The process as claimed in claim 1 , characterized in that it further comprises a step iv) of calcining said dried catalyst obtained in step iii) at a temperature of between 250 and 1000° C.3. The process as claimed in claim 1 , characterized ...

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

Disclosed are processes for conversion of a feedstock comprising C aromatic hydrocarbons to lighter aromatic products in which the feedstock and optionally hydrogen are contacted in the presence of a first and a second catalyst composition under conversion conditions effective to produce said lighter aromatic products comprising benzene, toluene and xylene. In the process, the C aromatic hydrocarbons are dealkylated to form C-Caromatic hydrocarbon and the C olefins formed are saturated. The remaining C aromatic hydrocarbons are transalkylated with the C-Caromatic hydrocarbon. The first and second catalyst compositions each comprise a zeolite, a first metal, and optionally a second metal, and are treated with a source of sulfur and/or a source of steam. 125.-. (canceled)27. The process of claim 26 , wherein said first catalyst composition and/or said second catalyst composition is treated with said source of sulfur in one or more stages at temperatures in the range 204° C. (400° F.) up to about 480° C. (900° F.).28. The process of claim 26 , wherein said source of sulfur is one or more of hydrogen sulfide claim 26 , carbon disulfide and alkylsulfides which are selected from the group consisting of methylsulfide claim 26 , dimethylsulfide claim 26 , dimethyldisulfide claim 26 , diethylsulfide claim 26 , dibutyl sulfide claim 26 , and mixtures of two or more thereof.29. The process of claim 26 , wherein said first zeolite and/or said second zeolite are treated with a source of steam.30. The process of claim 26 , wherein said source of steam comprises up to about 100% steam at temperatures in the range of about 260° C. (500° F.) to about 649° C. (1200° F.) and said treatment is in one or more temperature stages.31. The process of claim 26 , wherein said first metal of Group 6 is selected from the group consisting of chromium claim 26 , molybdenum claim 26 , tungsten and mixtures of two or more thereof.32. The process of claim 26 , wherein said second metal of Group 9 is ...

PREPARATION METHOD OF PLATINUM/TIN/METAL/ALUMINA CATALYST FOR DIRECT DEHYDROGENATION OF n-BUTANE AND METHOD FOR PRODUCING C4 OLEFINS USING SAID CATALYST

The provided is a method for preparing a platinum-tin-metal-alumina catalyst by comprising: as an active ingredient, platinum which has a high activity in a direct dehydrogenation reaction of n-butane, tin which can increase the catalyst stability by preventing carbon deposition; additionally metal for reducing the level of catalyst inactivation over the reaction time; and an alumina carrier for supporting said components. Further, provided is a method for producing a high value product, C4 olefins from low cost n-butane by using the catalyst prepared by the method according to the present invention in a direct dehydrogenation reaction.

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 ...

OXIDATIVE DEHYDROGENATION CATALYST COMPOSITIONS

Provided in this disclosure are catalyst compositions. The catalyst compositions include an oxidative dehydrogenation catalyst that includes a mixed metal oxide having the empirical formula: 1. A catalyst composition comprising an oxidative dehydrogenation catalyst comprising a mixed metal oxide having the empirical formula:{'br': None, 'sub': 1.0', '0.12-0.49', '0.05-0.25', '0.10-0.20', 'c', 'd, 'MoVTeNbAlO'} c is from 0 to 2.0,', 'd is a number to satisfy the valence of the oxide, and', 'the composition is at least 40 wt. % amorphous as measured by XRD., 'wherein2. The catalyst composition of claim 1 , wherein the composition is from 60 wt. % to 80 wt. % amorphous.3. The catalyst composition of claim 1 , wherein the composition further comprises an adjuvant.4. The catalyst composition of claim 3 , wherein the adjuvant comprises about 30 wt. % to about 90 wt. % of the catalyst composition.5. The catalyst composition of claim 4 , wherein the oxidative dehydrogenation catalyst comprises about 10 wt. % to about 70 wt. % of the catalyst composition.6. The catalyst composition of claim 1 , wherein the mixed metal oxide has the empirical formula:{'br': None, 'sub': 1.0', '0.12-0.49', '0.05-0.17', '0.10-0.20', 'c', 'd, 'MoVTeNbAlO'}wherein c is 0.01 to 2.0.7. The catalyst composition of claim 3 , wherein the adjuvant comprises an alumina.8. The catalyst composition of claim 7 , wherein the alumina comprises a boehmite.9. The catalyst composition of claim 1 , wherein the molar ratio of molybdenum to vanadium in the catalyst composition is from 1:0.12 to 1:0.49 claim 1 , the molar ratio of molybdenum to tellurium in the catalyst composition is from 1:0.05 to 1:0.25 claim 1 , the molar ratio of molybdenum to niobium in the catalyst composition is from 1:0.10 to 1:0.20 claim 1 , and the molar ratio of molybdenum to aluminum in the catalyst composition is from 0.01 to 2.0 claim 1 , as determined by PIXE.10. The catalyst composition of claim 1 , wherein the catalyst composition ...

MANGANESE-DOPED NICKEL METHANIZATION CATALYSTS HAVING ELEVATED SULPHUR RESISTANCE

A process for the methanation of carbon monoxide and/or carbon dioxide in a feed stream containing carbon monoxide and/or carbon dioxide is disclosed. This is achieved by a process for the methanation of carbon monoxide and/or carbon dioxide in a feed stream containing carbon monoxide and/or carbon dioxide, hydrogen and more than 1 ppb of sulfur, using a catalyst comprising aluminum oxide, an Ni active composition and Mn. It has surprisingly The Mn-containing Ni catalyst has a high sulfur resistance and also a high sulfur capacity. 1. A process for the methanation of carbon monoxide and/or carbon dioxide in a feed stream containing carbon monoxide and/or carbon dioxide , hydrogen and more than 1 ppb of sulfur , using a catalyst comprising aluminum oxide , an Ni active composition and Mn , wherein the molar ratio of Ni/Mn in the catalyst is in the range from 1.0 to 15.0 , preferably from 2.0 to 12.0.2. The process as claimed in claim 1 , wherein the catalyst has been produced by coprecipitation.3. The process as claimed in claim 1 , wherein the molar ratio of Ni/Mn in the catalyst is in the range from 2.0 to 6.0 or from 3.5 to 5.5.4. The process as claimed in claim 1 , wherein the molar ratio of Al/Ni in the catalyst is in the range from 0.1 to 0.9 claim 1 , preferably from 0.3 to 0.7.5. The process as claimed in claim 1 , wherein the catalyst has been produced by impregnation of aluminum oxide with a solution comprising Ni.6. The process as claimed in claim 5 , wherein the solution comprising Ni also contains Mn.7. The process as claimed in claim 5 , wherein the molar ratio of Ni/Mn in the catalyst is in the range from 6.0 to 10.0 claim 5 , particularly preferably from 7.5 to 9.5.8. The process as claimed in claim 5 , wherein the molar ratio of Al/Ni in the catalyst is in the range from 2 to 9 claim 5 , preferably from 2.3 to 5.9. The process as claimed in claim 1 , wherein the feed stream contains more than 1 ppb claim 1 , preferably more than 4 ppb claim 1 , ...

METHOD FOR PRODUCING INDENE

The present invention provides a production method for indene, comprising a dehydrogenation step of obtaining a reaction product containing indene by contacting a raw material composition containing indene with a dehydrogenation catalyst, wherein the dehydrogenation catalyst comprises a support containing aluminum, and a group 14 metal element and platinum supported on the support, a content of the platinum in the dehydrogenation catalyst is 0.6 to 2.5% by mass based on a whole amount of the dehydrogenation catalyst, and an atomic ratio of the group 14 metal element to the platinum in the dehydrogenation catalyst is 4.0 to 20.0. 1. A production method for indene , comprising a dehydrogenation step of obtaining a reaction product containing indene by contacting a raw material composition containing indane with a dehydrogenation catalyst ,wherein the dehydrogenation catalyst comprises a support containing aluminum, and a group 14 metal element and platinum supported on the support,a content of the platinum in the dehydrogenation catalyst is 0.6 to 2.5% by mass based on a whole amount of the dehydrogenation catalyst, andan atomic ratio of the group 14 metal element to the platinum in the dehydrogenation catalyst is 4.0 to 20.0.2. The production method according to claim 1 , wherein the atomic ratio of the group 14 metal element to the platinum in the dehydrogenation catalyst is 7.0 to 20.0.3. The production method according to claim 1 , wherein the group 14 metal element is tin.4. The production method according to claim 1 , wherein the group 14 metal element and the platinum are supported on the support by using a metal source not containing a chlorine atom.5. The production method according to claim 1 , wherein a mole fraction of the indane in the raw material composition is 0.2 or more.6. The production method according to claim 1 , further comprising a raw material synthesis step of obtaining indane by dehydrogenation reaction of tetrahydroindene. The present ...

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.

Microorganisms and methods for the biosynthesis of butadiene

The invention provides non-naturally occurring microbial organisms having a butadiene pathway. The invention additionally provides methods of using such organisms to produce butadiene.

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 ...

MICROORGANISMS AND METHODS FOR THE BIOSYNTHESIS OF BUTADIENE

The invention provides non-naturally occurring microbial organisms having a butadiene pathway. The invention additionally provides methods of using such organisms to produce butadiene. 1. A process for the production of butadiene comprising:(a) culturing by fermentation in a sufficient amount of nutrients and media a non-naturally occurring microbial organism that produces crotyl alcohol; and(b) converting crotyl alcohol produced by culturing said non-naturally occurring microbial organism to butadiene.2. The process of claim 1 , wherein step (b) is performed by chemical dehydration in the presence of a catalyst.3. The process of claim 1 , wherein said non-naturally occurring microbial organism comprises a crotyl alcohol pathway comprising at least one exogenous nucleic acid encoding a crotyl alcohol pathway enzyme expressed in a sufficient amount to produce crotyl alcohol claim 1 , said crotyl alcohol pathway comprising an acetyl-CoA:acetyl-CoA acyltransferase claim 1 , an acetoacetyl-CoA reductase claim 1 , a 3-hydroxybutyryl-CoA dehydratase claim 1 , a crotonyl-CoA reductase (aldehyde forming) claim 1 , a crotonaldehyde reductase (alcohol forming) claim 1 , a crotonyl-CoA hydrolase claim 1 , synthetase claim 1 , or transferase claim 1 , a crotonate reductase claim 1 , a crotonyl-CoA reductase (alcohol forming) claim 1 , a glutaconyl-CoA decarboxylase claim 1 , a glutaryl-CoA dehydrogenase claim 1 , a 3-aminobutyryl-CoA deaminase claim 1 , or a 4-hydroxybutyryl-CoA dehydratase.4. The process of claim 3 , wherein said microbial organism comprises two claim 3 , three or four exogenous nucleic acids each encoding a crotyl alcohol pathway enzyme.56-. (canceled)7. The process of claim 3 , wherein said crotyl alcohol pathway comprises a pathway selected from the group consisting of:an acetyl-CoA:acetyl-CoA acyltransferase, an acetoacetyl-CoA reductase, a 3-hydroxybutyryl-CoA dehydratase, a crotonyl-CoA reductase (aldehyde forming), and a crotonaldehyde reductase ( ...

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 ...

METHOD FOR PRODUCING ISOBUTYLENE FROM ISOBUTANOL

The purpose of the present invention is to provide a method that can produce, with high yield or high selectivity isobutylene by means of isobutanol dehydration-reaction. An isobutylene production method of a first embodiment of the present invention is a method for producing isobutylene by means of isobutanol dehydration-reaction, wherein isobutanol is reacted using a catalyst for which the BET specific surface area is within the range of 60 m/g-175 m/g, and the reaction is carried out under a reaction pressure of 50 kPa-750 kPa as the absolute pressure. An isobutylene production method of a second embodiment of the present invention includes: using a catalyst which is filled into a reaction chamber and for which the particle diameters of at least 90 mass % of the catalyst are within the range of 700 μm-1000 μm; setting the isobutanol concentration within a supplied reaction gas to 30 vol %-85 vol %; setting the weight hourly velocity (WHSV) of the isobutanol to 0.175 h˜20 h; and reacting isobutanol under a reaction pressure of 50 kPa-750 kPa as the absolute pressure. 1. A method for producing isobutylene by dehydration reaction of isobutanol , wherein isobutanol is reactedat a reaction pressure of 50 kPa or more and 750 kPa or less as an absolute pressure{'sup': 2', '2, 'by using a catalyst having a BET specific surface area in a range of 60 m/g or more and 175 m/g or less.'}2. A method for producing isobutylene by dehydration reaction of isobutanol , wherein isobutanol is reactedat a concentration of isobutanol in a reaction gas to be supplied of 30 vol % or more and 85 vol % or less,{'sup': −1', '−1, 'a weight hourly space velocity (WHSV) of isobutanol of 0.175 hor more and 20 hor less, and'}a reaction pressure of 50 kPa or more and 750 kPa or less as an absolute pressureby using a catalyst of which 90 mass % or more has a particle size in a range of 700 μm or more and 10000 pin or less.3. The method for producing isobutylene according to claim 1 , wherein 90 ...

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.

Transalkylated Cyclohexylbenzyl and Biphenyl Compounds

Processes for selectively alkylating and/or dealkylating one ring of cyclohexylbenzyl and/or biphenyl compounds are provided. Such selective alkylation and/or dealkylation takes place through a transalkylation reaction between the cyclohexylbenzyl compound and a substituted or unsubstituted benzene, which replaces the phenyl moiety of the cyclohexylbenzyl compound. The transalkylated cyclohexylbenzyl may be dehydrogenated to give a corresponding biphenyl compound. The same reaction steps can be utilized with respect to biphenyl compounds by first partially hydrogenating one phenyl ring of the biphenyl compound, thereby obtaining a corresponding cyclohexylbenzyl compound, which may undergo the transalkylation and, optionally, subsequent dehydrogenation. Combinations of any two or more of partial hydrogenation, transalkylation, and dehydrogenation enable targeted substitution (or de-substitution) of only one ring of cyclohexylbenzyl and/or biphenyl compounds, thereby providing superior control in designing the synthesis of these compounds. 5. The process of wherein R-Rare each H.6. The process of claim 5 , wherein R-Rare each H.7. The process of claim 1 , wherein one of R-Ris a C-Calkyl group claim 1 , and the rest of R-Rare each H; and further wherein R-Rare each H.8. The process of claim 1 , wherein the substituted or unsubstituted benzene and the additional substituted or unsubstituted benzene are each independently selected from the group consisting of toluene claim 1 , xylene claim 1 , and ethylbenzene.9. The process of claim 1 , wherein R*-R* and R*-R* each comprise the same five substitutions.10. The process of claim 3 , wherein the transalkylation catalyst and the second transalkylation catalyst are each independently selected from molecular sieves having a large pore molecular sieve having a Constraint Index less than 2.11. The process of claim 3 , wherein a single catalyst composition is both the transalkylation catalyst and the second transalkylation ...

METHODS AND APPARATUSES FOR ISOMERIZATION OF PARAFFINS

Embodiments of methods and apparatuses for isomerization of paraffins are provided. In one example, a method comprises the steps of separating an isomerization effluent into a product stream that comprises branched paraffins and a stabilizer overhead vapor stream that comprises HCl, H, and C-hydrocarbons. C-hydrocarbons are removed from at least a portion of the stabilizer overhead vapor stream to form a HCl and H-rich stream. An isomerization catalyst is activated using at least a portion of the HCl and H-rich stream to form a chloride-promoted isomerization catalyst. A paraffin feed stream is contacted with the chloride-promoted isomerization catalyst in the presence of hydrogen for isomerization of the paraffins. 1. A method for isomerization of paraffins , the method comprising the steps of:{'b': 42', '44', '46, 'sub': 2', '6, 'separating an isomerization effluent () into a product stream () that comprises branched and un-branched paraffins and a stabilizer overhead vapor stream () that comprises HCl, H, and C-hydrocarbons;'}{'sub': 6', '2, 'b': 46', '40, 'removing C-hydrocarbons from at least a portion of the stabilizer overhead vapor stream () to form a HCl and H-rich stream ();'}{'sub': '2', 'b': '40', 'activating an isomerization catalyst using at least a portion of the HCl and H-rich stream () to form a chloride-promoted isomerization catalyst; and'}{'b': '22', 'contacting a paraffin feed stream () with the chloride-promoted isomerization catalyst in the presence of hydrogen for isomerization of the paraffins.'}2465462. The method of claim 1 , wherein the step of removing comprises separating the stabilizer overhead vapor stream () at first separation conditions effective to form a liquid stream () that comprises Chydrocarbon and a net gas stream () that comprises HCl claim 1 , H claim 1 , and C-hydrocarbons.346. The method of claim 2 , wherein the step of removing comprises separating the stabilizer overhead vapor stream () at the first separation ...

PROCESS FOR PREPARING A CATALYST FOR THE HYDROGENATION OF AROMATICS, COMPRISING A STEP OF FORMING A NI-CU ALLOY IN PRE-IMPREGNATION

A process for preparing a catalyst for the hydrogenation of aromatic or polyaromatic compounds comprising nickel, copper and a support comprising at least one refractory oxide, comprising the following steps: 1. A process for preparing a catalyst for the hydrogenation of aromatic or polyaromatic compounds comprising nickel , in a proportion of 10% and 65% by weight of nickel element relative to the total weight of the catalyst , and copper , in a proportion of 0.5% to 15% by weight of copper element relative to the total weight of the catalyst , and a support comprising at least one refractory oxide chosen from silica , alumina and silica-alumina , said process comprising the following steps:a) a step of bringing the support into contact with at least one solution containing at least one copper precursor and one nickel precursor at a desired nickel concentration is carried out in order to obtain, on the final catalyst, a content of between 0.5% and 15% by weight of nickel element relative to the total weight of the final catalyst;b) at least one step of drying the catalyst precursor resulting from step a) is carried out at a temperature of less than 250° C.;c) optionally, a heat treatment of the catalyst precursor obtained at the end of step b) is carried out at a temperature of between 250 and 1000° C., in the presence or absence of water;d) the catalyst precursor resulting from step b), optionally step c), is reduced by bringing said catalyst precursor into contact with a reducing gas at a temperature of between 150 and 250° C.;e) a step of bringing the catalyst precursor obtained at the end of step d) into contact with a solution comprising at least one nickel precursor is carried out;f) at least one step of drying the catalyst precursor resulting from step e) is carried out at a temperature of less than 250° C.;g) optionally, a heat treatment of the catalyst precursor obtained at the end of step f) is carried out at a temperature of between 250 and 1000° C., in ...

UNSATURATED HYDROCARBON PRODUCTION METHOD AND CONJUGATED DIENE PRODUCTION METHOD

A method for producing a conjugated diene according to an aspect of the present invention comprises a step of contacting a raw material gas containing an alkane with a dehydrogenation catalyst to obtain a product gas containing at least one unsaturated hydrocarbon selected from the group consisting of an olefin and a conjugated diene. In the production method, the dehydrogenation catalyst is a catalyst having a supported metal containing a Group 14 metal element and Pt supported on a support containing Al and a Group 2 metal element; the dehydrogenation catalyst has pores (a) having a pore diameter of 7 nm or more and 32 nm or less; and a proportion of a pore volume of the pores (a) is 65% or more of the total pore volume of the dehydrogenation catalyst. 1. A method for producing an unsaturated hydrocarbon , comprising a step of contacting a raw material gas containing an alkane with a dehydrogenation catalyst to obtain a product gas containing at least one unsaturated hydrocarbon selected from the group consisting of an olefin and a conjugated diene ,wherein:the dehydrogenation catalyst is a catalyst having a supported metal containing a Group 14 metal element and Pt supported on a support containing Al and a Group 2 metal element,the dehydrogenation catalyst has pores (a) having a pore diameter of 7 nm or more and 32 nm or less, anda proportion of a pore volume of the pores (a) is 65% or more of the total pore volume of the dehydrogenation catalyst.2. The production method according to claim 1 , wherein the proportion of the pore volume of the pores (a) is 70% or more of the total pore volume of the dehydrogenation catalyst.3. The production method according to claim 1 , wherein the Group 14 metal element is Sn.4. The production method according to claim 1 , wherein the Group 2 metal element is Mg.5. The production method according to claim 1 , wherein the alkane is an alkane having 4 to 10 carbon atoms.6. The production method according to claim 1 , wherein the ...

ALKYLATE BASE OIL OF BIOLOGICAL ORIGIN

An alkylate base oil of a biological origin having a kinematic viscosity at 100° C. from 3 mm/s to 20 mm/s, and characterized by having a total integral of a C NMR spectrum wherein 25-60% of the total integral of the C NMR spectrum falls within C NMR resonances in ranges for linear long chain alkyl groups given by: C1(13.9-14.2 ppm), C2(22.6-22.8 ppm), C3(31.9-32.05 ppm), C4(29.35-29.45 ppm), and C5+(29.6-29.8 ppm). 1. An alkylate base oil of a biological origin having a kinematic viscosity at 100° C. from 3 mm/s to 20 mm/s , and characterized by having a total integral of a C NMR spectrum wherein 25-60% of the total integral of the C NMR spectrum falls within C NMR resonances in ranges for linear long chain alkyl groups given by: C1(13.9-14.2 ppm) , C2(22.6-22.8 ppm) , C3(31.9-32.05 ppm) , C4(29.35-29.45 ppm) , and C5+(29.6-29.8 ppm).2. The alkylate base oil of claim 1 , additionally having a viscosity index of 50 to 140.3. The alkylate base oil of claim 1 , additionally having a viscosity index of 80 or greater.4. The alkylate base oil of claim 1 , wherein the alkylate base oil is saturated.5. The alkylate base oil of claim 1 , additionally having a bromine index less than 500 mg Br/100 g.6. The alkylate base oil of claim 5 , wherein the bromine index is less than 100 mg Br/100 g.7. The alkylate base oil of claim 1 , additionally having a long straight backbone with two long chain alkyl ends.8. The alkylate base oil of claim 1 , additionally having a pour point less than −15° C.9. The alkylate base oil of claim 1 , additionally having a cloud point less than −20° C.10. The alkylate base oil of claim 1 , wherein the biological origin is at least 95%.11. The alkylate base oil of claim 1 , wherein the alkylate base oil of the biological origin is an alkylation product of a farnesane that was made from a biologically derived feedstock.12. A finished lubricant claim 1 , comprising: the alkylate base oil of and at least one additive selected from the group consisting of ...

DIENE PRODUCTION METHOD

A method for producing diene in which diene can be produced in a high yield by using a raw material including a branched olefin and a straight chain olefin is provided. The method for producing diene comprises: a step 1 of obtaining an internal olefin by removing a branched olefin from a raw material including at least the branched olefin and a straight chain olefin; a step 2 of isomerizing the internal olefin to a terminal olefin by using an isomerization catalyst; and a step 3 of producing diene from the terminal olefin obtained in the step 2 by oxidative dehydrogenation using a dehydrogenation catalyst. 1. A method for producing diene , comprising:a step 1 of obtaining an internal olefin by removing a branched olefin from a raw material including at least the branched olefin and a straight chain olefin;a step 2 of isomerizing the internal olefin to a terminal olefin by using an isomerization catalyst; anda step 3 of producing diene from the terminal olefin obtained in the step 2 by oxidative dehydrogenation using a dehydrogenation catalyst.2. The method for producing diene according to claim 1 ,wherein at least a part of the straight chain olefin is a terminal olefin, andwherein in the step 1, the branched olefin is removed from the raw material and the terminal olefin is isomerized to the internal olefin by reactive distillation.3. The method for producing diene according to claim 1 ,wherein the isomerization catalyst includes at least one selected from the group consisting of silica and alumina.4. The method for producing diene according to claim 1 ,wherein the dehydrogenation catalyst has a complex oxide including bismuth, molybdenum and oxygen.5. The method for producing diene according to claim 1 ,wherein in the step 2, the internal olefin is isomerized to the terminal olefin to obtain a first fraction including the terminal olefin and a second fraction including an unreacted portion of the internal olefin by reactive distillation.6. The method for producing ...

Catalyst for oxidative dehydrogenation reaction, and method for producing same

Provided is a catalyst for an oxidative dehydrogenation reaction that comprises: a porous support; a core portion supported on the porous support and containing a first zinc ferrite-based catalyst; and a shell portion supported on the core portion and containing a second zinc ferrite-based catalyst, in which the first zinc ferrite-based catalyst and the second zinc ferrite-based catalyst are different from each other.

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 ...

Process for performing an endothermic reaction

Process for performing an endothermic reaction in a reactor containing catalyst tubes, the catalyst tubes containing a catalyst promoting the endothermic reaction, the process comprising the steps of, a. contacting the catalyst contained in the catalyst tubes with a feed flow passing through the channels from an entrance end to an exit end, b. contacting an outer surface of the catalyst tubes with a flow of a heating medium having an initial heating temperature and flowing co-currently with the flow of feeds to heat the surface by convection, c. mixing at least part of the heating medium after having been contacted with the catalyst tubes with a flow of fresh heating medium having a start temperature higher than the initial heating temperature to form the co-current heating medium having the initial heating temperature and reactor for carrying out the process.

Counter-Current Fluidized Bed Reactor for the Dehydrogenation of Olefins

A process and apparatus for the dehydrogenation of paraffins is presented. The process utilizes a reactor that includes a slower flow of catalyst through the reactor, with a counter current flow of gas through the catalyst bed. The catalyst is regenerated and distributed over the top of the catalyst bed, and travels through the bed with the aid of reactor internals to limit backmixing 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 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 ...

UZM-53, AN MTT ZEOLITE

A new crystalline aluminosilicate zeolite comprising a MTT framework has been synthesized that has been designated UZM-53. This zeolite is represented by the empirical formula: 2. The zeolite of wherein two peaks of very strong intensity are present.3. The zeolite of wherein said zeolite has a y in said empirical formula that is less than 25.4. The zeolite of wherein said zeolite has a y in said empirical formula that is less than 22.6. The zeolite of wherein in said empirical formula for said zeolite claim 5 , y′ is from about 12 to 25.7. The zeolite of wherein said zeolite has a NHLewis acid value of less than 0.05.8. The zeolite of wherein said zeolite has a NHLewis acid value of less than 0.04.9. The zeolite of wherein said zeolite has a NHLewis acid value of less than 0.03.10. The zeolite of wherein said zeolite has a Collidine Brønsted value of less than 0.12.11. The zeolite of wherein said zeolite has a Collidine Brønsted value of less than 0.113. The process of where M is a combination of sodium and potassium and the ratio of sodium to potassium is in the range from about 0.1 to about 2.14. The process of where the source of E is selected from the group consisting of alkali borates claim 12 , boric acid claim 12 , precipitated gallium oxyhydroxide claim 12 , gallium sulfate claim 12 , ferric sulfate claim 12 , ferric chloride and mixtures thereof.15. The process of where the aluminum source is selected from the group consisting of aluminum alkoxides claim 12 , precipitated aluminas claim 12 , aluminum metal claim 12 , aluminum hydroxide claim 12 , sodium aluminate claim 12 , potassium aluminate claim 12 , aluminum salts and aluminum sols.16. The process of where the silicon source is selected from the group consisting of tetraethylorthosilicate claim 12 , fumed silica claim 12 , colloidal silica claim 12 , alkali silicates and precipitated silica.17. The process of further comprising adding UZM-53 seeds to the reaction mixture.18. The process of wherein the ...

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 ...

LINEAR ALKYLBENZENES FROM NATURAL OILS AND METHODS OF PRODUCING

The production of linear alkylbenzene from a natural oil is provided. A method comprises the step of deoxygenating the natural oils to form a stream comprising paraffins. The paraffins are dehydrogenated to provide mono-olefins. Then, benzene is alkylated with the mono-olefins under alkylation conditions to provide an alkylation effluent comprising alkylbenzenes and benzene. Thereafter, the alkylbenzenes are isolated to provide the alkylbenzene product. 1. A method for generating an alkylbenzene product from a natural oil comprising:deoxygenating feedstock comprising natural oil having less than about 3 wt. ppm of nitrogen contained in nitrogen containing compounds to form a stream comprising paraffins;dehydrogenating at least a portion of the paraffins to provide mono-olefins;alkylating benzene with the mono-olefins under alkylation conditions to provide an alkylation effluent comprising alkylbenzenes and benzene;separating the alkylbenzenes to provide the alkylbenzene product comprising alkylbenzenes having an alkyl group of about n carbon atoms where n is from 12 to about 13 and wherein the alkyl group is a linear alkyl group for for at least 80 mass % of the alkylbenzenes having an alkyl group of about n carbon atoms.2. The alkylbenzene product produced by the method of .31. The method of further comprising claim 1 , sulfonating the alkylbenzene product to form a linear alkylbenzene sulfonate product.4. The linear alkylbenzene sulfonate product produced by the method of .5. The method of further comprising where n is expanded to include from 8 to 15.6. The method of further comprising where n is expanded to include from 10 to 13.7. The method of further comprising where n is expanded to include from 9 to 14.8. The method of wherein a hydrogen stream results from dehydrogenating the paraffins claim 1 , and wherein the method further comprises recycling the hydrogen stream to the deoxygenating step.9. The method of further comprising separating a second portion of ...

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 ...

Process for Nitrile Removal from Hydrocarbon Feeds

A process is described, such process comprising i) contacting a hydrocarbon feed with a heterogeneous catalyst under conditions suitable to hydrolyze nitriles present in the feed to form a nitrile hydrolysis product comprising ammonia, carboxylic acid and carboxylate salts or a mixture thereof; and ii) removing the nitrile hydrolysis product from the feed. In an embodiment, the hydrocarbon feed comprises olefins and is intended for use in an olefin oligomerization process.

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 ...

SUPPORTED CORE-SHELL STRUCTURED ZnO CATALYST, AND PREPARATION METHOD AND USE THEREOF

The present invention belongs to the technical field of supported catalysts, and discloses a supported core-shell structured ZnO catalyst, and a preparation method and use thereof. With AlOas a support and ZnO as active sites, the catalyst is characteristic of a NiZn@ZnO core-shell structure, which consists of a NiZn alloy core and a ZnO shell The preparation method comprises firstly dissolving Ni(NO).6HO and Zn(NO).6HO in deionized water; then impregnating AlOwith the solution described above, followed by uniform ultrasonic dispersion and complete drying; and finally the obtained solid is calcinated and reduced to obtain the target catalyst, which exhibits high activity, selectivity and stability. The catalyst can be used for the dehydrogenation of light alkanes to alkenes, especially in dehydrogenation of propane to propylene. 1. A supported core-shell structured ZnO catalyst , wherein the catalyst is composed of AlOas a support and ZnO as active sites; a NiZn@ZnO core-shell structure , which consists of a NiZn alloy core and a ZnO shell , is supported on the AlO , denoted as NixZny/AlO , wherein x:y=(1:1)-(1:4) , representing the molar ration of Ni/Zn.2. The supported core-shell structured ZnO catalyst according to claim 1 , wherein the catalyst contains 1%-3% of Ni based on the mass of the AlOsupport.3. The supported core-shell structured ZnO catalyst according to claim 2 , wherein the catalyst contains 0.5%-6% of Ni based on the mass of the AlOsupport.4. The supported core-shell structured ZnO catalyst according to claim 1 , wherein x:y=1:3.5. A method for preparing the supported core-shell structured ZnO catalyst according to claim 1 , wherein the method comprises the following steps:{'sub': ['3', '3', '2', '3', '2', '2'], '#text': '(1) dissolving Ni(NO).6HO and Zn(NO).6HO in deionized water;'}{'sub': ['2', '3'], '#text': '(2) impregnating AlOwith the solution obtained in step (1), followed by uniform ultrasonic dispersion and complete drying; and'}{'sub': ['2 ...

HYDROALKYLATION OF MONONUCLEAR AROMATIC HYDROCARBONS TO MONO CYCLOALKYL AROMATIC HYDROCARBONS

An aspect of the present disclosure relates to a process for preparing a composite hydroalkylation catalyst including: (a) effecting impregnation of a hydrogenation metal on an inorganic oxide to form a metal impregnated inorganic oxide; (b) effecting calcination of the metal impregnated inorganic oxide to obtain a calcined metal impregnated inorganic oxide; (c) preparing a composite mixture comprising a molecular sieve, the calcined metal impregnated inorganic oxide and a binder; (d) preparing an extruded catalyst; and (e) effecting calcination of the extruded catalyst to obtain the composite hydroalkylation catalyst. The composite hydroalkylation catalyst prepared using this process affords dramatic improvement in conversion of mononuclear aromatic hydrocarbon and the yield of the hydroalkyled mononuclear aromatic hydrocarbon (e.g. CHB). 1. A process for preparing a composite hydroalkylation catalyst , said process comprising the steps of:(a) effecting impregnation of a hydrogenation metal on an inorganic oxide to form a metal impregnated inorganic oxide;(b) effecting calcination of the metal impregnated inorganic oxide at a temperature ranging from 250° C. to 500° C. for a time period ranging from 1 hour to 15 hours to obtain a calcined metal impregnated inorganic oxide;(c) preparing a composite mixture comprising a molecular sieve, the calcined metal impregnated inorganic oxide and a binder;(d) kneading the composite mixture to obtain an extruded catalyst; and(e) effecting calcination of the extruded catalyst at a temperature ranging from 250° C. to 400° C. to obtain the composite hydroalkylation catalyst.2. The method as claimed in claim 1 , wherein the composite hydroalkylation catalyst is subjected to reduction at a temperature ranging from 200° C. to 500° C. for a time period ranging from 3 hours to 20 hours.3. The method as claimed in claim 1 , wherein said composite mixture comprises the molecular sieve claim 1 , the calcined metal impregnated inorganic ...

CATALYST FOR ISOBUTYLENE PRODUCTION AND METHOD FOR PRODUCING ISOBUTYLENE

Provided are: a catalyst for dehydration, with which isobutylene is able to be produced with high conversion and high selectivity through a dehydration reaction of isobutanol; and a method for producing isobutylene. This catalyst has a BET specific surface area within the range of from 210 m/g to 350 m/g (inclusive) as calculated from Nadsorption/desorption isotherms. It is preferable that this catalyst is formed of at least one substance selected from among alumina, silica alumina, zeolite, and solid phosphoric acid. It is more preferable that this catalyst contains alumina, and it is especially preferable that this catalyst is formed of alumina. In this method for producing isobutylene, the isobutanol concentration in the starting material gas is preferably 20% by volume or more, more preferably 40% by volume or more, and especially preferably 60% by volume or more. In addition, the temperature of a catalyst layer is preferably from 230° C. to 370° C. (inclusive), and more preferably from 240° C. to 360° C. (inclusive). 1: A catalyst for dehydration used for producing isobutylene by a dehydration reaction of isobutanol , the catalyst having a BET specific surface area , which is calculated from Nadsorption/desorption isotherms , within a range of from 210 m/g to 350 m/g.2: The catalyst according to claim 1 , which is at least one catalyst selected from the group consisting of alumina claim 1 , silica alumina claim 1 , zeolite claim 1 , and solid phosphoric acid.3: The catalyst according to claim 1 , comprising alumina.4: The catalyst according to claim 1 , which is alumina.5: The catalyst according to claim 1 , wherein the specific surface area of the catalyst is from 215 m/g to 350 m/g.6: The catalyst according to claim 1 , wherein the specific surface area of the catalyst is from 220 m/g to 350 m/g.7: The catalyst according to claim 1 , wherein the specific surface area of the catalyst is from 225 m/g to 350 m/g.8: The catalyst according to claim 1 , wherein the ...

Enhanced performance of the dehydrogenation by the reduction of coke formation using pre-activated co2

The present disclosure addresses the deficiencies described above by providing systems and methods for enhancing the efficiency and yield of alkene production. The methods and systems provide for the use of activated CO 2 in a dehydrogenation reactor along with an alkane stream. Through the use of the methods and systems of the invention, catalyst deactivation by coke deposition is reduced and the selectivity and efficiency of the dehydrogenation reaction is improved.

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 ...