СЕЛЕКТИВНОЕ ПОЛУЧЕНИЕ ПАРА-КСИЛОЛА ПОСРЕДСТВОМ МЕТИЛИРОВАНИЯ ТОЛУОЛА

Изобретение относится к способу селективного получения параксилола, который включает взаимодействие толуола с метанолом в присутствии катализатора, содержащего пористый кристаллический алюмосиликатный цеолит, имеющий параметр диффузии по 2,2-диметилбутану примерно 0,1-15 с-1, измеренный при температуре 120oС и давлении 2,2-диметилбутана (8 кПа). Пористый кристаллический материал предпочтительно представляет собой цеолит со средним размером пор, в частности ZSM-5, который подвергают обработке водяным паром в жестких условиях при температуре, по меньшей мере, 1000oС. Алюмосиликатный цеолитный катализатор предпочтительно объединяют с, по меньшей мере, одним оксидным модификатором, предпочтительно содержащим фосфор, чтобы регулировать снижение объема микропор материала в ходе стадии обработки паром. Технический результат - увеличение выхода продукта, упрощение технологии процесса. 2 с. и 15 з.п. ф-лы, 10 табл., 3 ил.

СПОСОБ ПРЕВРАЩЕНИЯ ОЛЕФИНА ИЛИ СПИРТА И СПОСОБ ПОЛУЧЕНИЯ ПРОПИЛЕНА ИЛИ АРОМАТИЧЕСКОГО СОЕДИНЕНИЯ

Изобретение относится к способу превращения олефина или спирта и способу получения пропилена или ароматического соединения. Способ превращения олефина или спирта включает этап предварительной обработки, в котором получают проводящий катализатор путем загрузки реактора с псевдоожиженным слоем непроводящим катализатором, содержащим цеолит и/или оксид кремния, и подачи нагретого углеводородного газа в реактор с псевдоожиженным слоем для осаждения углеродистого кокса и нанесения на непроводящий катализатор, и этап превращения олефина или спирта с помощью реакции в псевдоожиженном слое, в котором используют данный проводящий катализатор, где скорость подачи газа составляет 0,40 м/с или менее на стадии предварительной обработки в виде скорости потока газа в реакторе с псевдоожиженным слоем, и скорость подачи газа составляет 0,5 м/с или более на стадии превращения олефина или спирта в виде скорости потока газа в реакторе с псевдоожиженным слоем. Изобретение обеспечивает подавление электростатического ...

РЕГЕНЕРАЦИЯ СОДЕРЖАЩИХ МЕТАЛЛ КАТАЛИЗАТОРОВ

Изобретение относится к способу регенерации закоксованного содержащего металл катализатора. Способ включает взаимодействие закоксованного содержащего металл катализатора в зоне регенерации с атмосферой, которая содержит диоксид углерода и монооксид углерода, где отношение парциального давления монооксида углерода к парциальному давлению диоксида углерода в зоне регенерации составляет от 2,3:1 до 100:1, и которая содержит менее 100 част./млн молекулярного кислорода, при температуре, равной от 600°С до 900°С, в течение времени, равного от примерно 0,1 до примерно 60 мин, причем способ дополнительно включает взаимодействие закоксованного содержащего металл катализатора в зоне регенерации с атмосферой, которая содержит водород, при температуре, равной не ниже 400°С, одновременно с указанным взаимодействием с указанной атмосферой, содержащей диоксид углерода и монооксид углерода, или после него. Технический результат заключается в разработке способа регенерации, который является эффективным ...

СПОСОБ КОНВЕРСИИ УГЛЕВОДОРОДОВ С ИСПОЛЬЗОВАНИЕМ СВЯЗАННОГО ЦЕОЛИТОМ ЦЕОЛИТНОГО КАТАЛИЗАТОРА

Использование: в нефтехимии. Сущность: углеводородное сырье контактирует в условиях конверсии углеводородов со связанным цеолитом цеолитным катализатором, включающим (а) первые кристаллы первого цеолита и (б) связующее вещество, содержащее вторые кристаллы второго цеолита, средний размер частиц которых меньше размера первых кристаллов, причем вторые кристаллы находятся в сращенном состоянии с первыми кристаллами и образуют на них покрытие или частичное покрытие. Технический результат - повышение селективности процесса. 50 з.п. ф-лы, 8 табл., 4 ил.

СПОСОБ ПОЛУЧЕНИЯ ЛЕГКИХ ОЛЕФИНОВ

Изобретение относится к способу получения легких олефинов, где в способе получения легких олефинов путем непрерывного контактирования сырья на основе кислородсодержащих соединений и катализатора для осуществления реакции дегидратации реакционное давление Р реакции дегидратации находится в диапазоне 1,2-2,8 МПа, среднечасовая скорость подачи сырья Н в реакцию дегидратации находится в диапазоне 7-250 час, где в ходе реакции дегидратации Н и Р удовлетворяют математической функции H=f(P), которая является строго возрастающей функцией. Способ получения легких олефинов реализуется в простом и непрерывном производственном процессе, приводит к значительному увеличению производства легких олефинов и характеризуется высокой безопасностью. 14 з.п. ф-лы, 3 пр., 6 табл., 7 ил.

СПОСОБ ПОЛУЧЕНИЯ АРОМАТИЧЕСКИХ СОЕДИНЕНИЙ

Изобретение относится к способу получения низкомолекулярных ароматических соединений. Способ получения низкомолекулярных ароматических соединений из черного щелока включает: предоставление черного щелока, который является производным от щелочной обработки древесной щепы, где древесная щепа является производной от твердой древесины; подвергание черного щелока обработке пиролизом, чтобы получить от пиролизованного черного щелока газ и массив твердотельного вещества, содержащий обуглившееся вещество и соли, в первом реакторе, где соли являются, в основном, производными от обработки черного щелока; приведение по меньшей мере части газа от пиролизованного черного щелока в контактирование с катализатором во втором реакторе, который отличается от первого реактора, чтобы предоставить конверсионную обработку для получения на выходе продукта конверсии; извлечение низкомолекулярных ароматических соединений из продукта конверсии. Технический результат – более высокий суммарный выход низкомолекулярных ...

ПОЛУЧЕНИЕ КАТАЛИЗАТОРА НА ОСНОВЕ ZSM-5; ИСПОЛЬЗОВАНИЕ В СПОСОБЕ ДЕАЛКИЛИРОВАНИЯ ЭТИЛБЕНЗОЛА

Изобретение относится к способу получения каталитической композиции и к способу конверсии ароматических углеводородов, содержащих исходное сырье, с использованием каталитической композиции, полученной таким способом. Способ получения каталитической композиции включает стадии: (а) обработки цеолита ZSM-5 щелочным раствором, содержащим гидроксид металла и имеющим рН по меньшей мере 8, с получением обработанного щелочным раствором цеолита, с последующим промыванием водой и сушкой, а затем подвергания обработанного щелочным раствором цеолита ионному обмену путем обработки цеолита раствором, содержащим соль аммония, для получения обработанного цеолита, (b) экструдирования смеси обработанного цеолита и связующего, где связующее представляет собой огнеупорный оксид, выбранный из группы, состоящей из диоксида кремния, диоксида циркония, диоксида титана и их смесей, и приведение в контакт цеолита с раствором, содержащим фторсодержащее соединение, причем раствор, содержащий фторсодержащее соединение ...

КАТАЛИЗАТОР НА ОСНОВЕ ZSM-5

Изобретение относится к микросферам цеолита ZSM-5 для применения в качестве катализатора, компонента катализатора или промежуточного продукта катализатора для процессов конверсии углеводородов, сформированным 1) формированием смеси в микросферах, в которых смесь содержит материал на основе диоксида кремния и множества частиц, выбранных из группы, включающей по меньшей мере один материал высокой плотности с абсолютной объемной плотностью по меньшей мере 0.3 г/см, кристаллы цеолита ZSM-5 и их комбинации; 2) прокаливанием микросфер и 3) взаимодействием и последующим нагреванием микросфер по меньшей мере с одним щелочным раствором, чтобы сформировать цеолит ZSM-5 in situ на микросферах, при этом микросферы цеолита ZSM-5 содержат не более чем 8 мас.% глины или прокаленного глинистого материала. Технический результат заключается в получении in situ катализатора из цеолита ZSM-5 с высокой устойчивостью к истиранию с микросферами, практически не содержащими глиняные загустители и/или ZSM-5. 2 н ...

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 ...

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 АЛКИЛИРОВАНИЯ АРОМАТИЧЕСКИХ СОЕДИНЕНИЙ

Изобретение относится к двум вариантам способа алкилирования ароматических соединений. Один из вариантов включает: (a) пропускание ароматического углеводородного сырья, содержащего поток рециркулируемого ароматического углеводорода и необязательно свежий ароматический углеводород, через блок обработки, содержащий адсорбент из глины, при таких условиях, чтобы адсорбент из глины удалял примеси, содержащиеся в ароматическом углеводородном сырье, с получением потока обработанного ароматического углеводорода, при этом обработку проводят при температуре от 40°C до менее чем 130°C; (b) подачу по меньшей мере части указанного потока обработанного ароматического углеводорода в зону алкилирования; (c) контактирование указанного потока обработанного ароматического углеводорода в указанной зоне алкилирования с алкилирующим агентом в присутствии кислотного катализатора алкилирования и при таких условиях, чтобы по меньшей мере часть алкилирующего агента вступала в реакцию с указанным потоком обработанного ...

КАТАЛИЗАТОР ДЛЯ ПРЕОБРАЗОВАНИЯ УГЛЕВОДОРОДОВ И СПОСОБ ПОЛУЧЕНИЯ НИЗШИХ ОЛЕФИНОВ И МОНОЦИКЛИЧЕСКИХ АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ

Катализатор для преобразования углеводородов содержит цеолит с содержанием протонов 0,02 ммоль/г цеолита или менее, при соотношении SiO2 к Аl2О3 20 -500, диаметре пор 5-6,5 Катализатор устойчив при 550-750oС, что способствует получению олефинов, содержащих этилен в качестве основного компонента, и моноциклических ароматических углеводородов при хорошем соотношении и высоком выходе. 3 с. и 4 з.п. ф-лы, 10 табл.

СПОСОБ IN-SITU ПОЛУЧЕНИЯ КАТАЛИЗАТОРА ДЛЯ ПОЛУЧЕНИЯ ПО МЕНЬШЕЙ МЕРЕ ОДНОГО ИЗ ТОЛУОЛА, ПАРА-КСИЛОЛА И НИЗШИХ ОЛЕФИНОВ, А ТАКЖЕ ПРОЦЕСС РЕАКЦИИ

Настоящее изобретение относится к способу in-situ получения катализатора для получения по меньшей мере одного из толуола, пара-ксилола и низших олефинов, а также к процессу реакции получения по меньшей мере одного из толуола, пара-ксилола и низших олефинов, и относится к области химической технологии. Описан способ in-situ получения катализатора, в котором модификатор приводят в контакт с цеолитным молекулярным ситом в реакторе для in-situ получения катализатора для получения пара-ксилола, толуола и/или низших олефинов из сырьевого материала, содержащего метанол и/или диметиловый эфир; и реактор представляет собой реактор для получения пара-ксилола, толуола и/или низших олефинов из сырьевого материала, содержащего метанол и/или диметиловый эфир; при этом модификатор содержит по меньшей мере один из следующих модификаторов: Модификатор I: фосфорсодержащий реагент и силилирующий реагент; Модификатор II: силилирующий реагент; Модификатор III: силилирующий реагент и водяной пар; Модификатор ...

РЕАКТОР С КИПЯЩИМ СЛОЕМ И СПОСОБ ПОЛУЧЕНИЯ ПАРА-КСИЛОЛА И СОВМЕСТНОГО ПОЛУЧЕНИЯ НИЗШИХ ОЛЕФИНОВ ИЗ БЕНЗОЛА И МЕТАНОЛА И/ИЛИ ДИМЕТИЛОВОГО ЭФИРА

Изобретение относится к реакторам с кипящим слоем и их использованию для получения пара-ксилола и совместного получения низших олефинов из бензола и метанола и/или диметилового эфира. Описан реактор, содержащий первый и второй распределитель, через которые в реактор поступают материальные потоки A и В, причем первый распределитель расположен в нижней части кипящего слоя, а второй расположен в по меньшей мере одной зоне газового потока после первого распределителя; причем второй распределитель содержит впускную трубу, микропористую трубу и впускную кольцевую трубу; впускная труба соединена с газовым каналом микропористой трубы, причем газ подают через впускную трубу снаружи от кипящего слоя в микропористую трубу в кипящем слое; впускная кольцевая труба соединена с газовым каналом впускной трубы, причем впускная кольцевая труба расположена в плоскости, перпендикулярной направлению потока газа из первого распределителя; микропористая труба расположена на кольцевой впускной трубе и перпендикулярно ...

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 ...

КАТАЛИЗАТОР, СПОСОБ ЕГО ПРИГОТОВЛЕНИЯ И СПОСОБ ПОЛУЧЕНИЯ СМЕСИ УГЛЕВОДОРОДОВ С НИЗКИМ СОДЕРЖАНИЕМ АРОМАТИЧЕСКИХ СОЕДИНЕНИЙ

Изобретение относится к катализаторам получения углеводородов. Описан катализатор синтеза смеси углеводород с низким содержанием ароматических углеводородов на основе кристаллического алюмосиликата - цеолита типа пентасилов с SiO2/Al2O3=25-100, содержащего не более 0,1 мас.% оксида натрия, оксид цинка, палладий и связующее, причем он дополнительно содержит оксид циркония и/или оксид лантана при следующих соотношениях компонентов, мас.%: оксид цинка - 0,5-2,0; оксид циркония - 0,2-1,0; и/или оксид лантана - 0,2-1,0; палладий - 0,1-1,0; указанный цеолит - 65,0; связующее - остальное. Описан также способ получения катализатора синтеза смесей углеводородов с низким содержанием ароматических углеводородов по п.1, включающий модифицирование цеолитов типа пентасилов с SiO2/Al2O3=25-100, содержащего не более 0,1 мас.% оксида натрия, оксидом цинка и палладия, смешение со связующим, формование экструдатов, их сушку и прокаливание, в котором аммонийную форму цеолита сначала модифицируют водными растворами ...

КАТАЛИЗАТОР И СПОСОБ СИНТЕЗА АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ ПУТЕМ ПРЯМОЙ КОНВЕРСИИ СИНТЕЗ-ГАЗА

Настоящее изобретение относится к технологии синтеза ароматических углеводородов из синтез-газа, в частности, относится к катализатору и способу синтеза ароматических углеводородов путем прямой конверсии синтез-газа. В способе синтез-газ используется как сырье, и способ осуществляется в реакторе с неподвижным слоем или с движущимся слоем. Давление синтез-газа составляет 0,1-6 МПа, температура реакции составляет 300-600°C, и объемная скорость составляет 500-8000 ч. В качестве катализатора используют катализатор, который является составным катализатором, состоящим из компонентов A и B и образованным компаундированием каталитического компонента A и каталитического компонента B в режиме механического смешения. Активной составляющей каталитического компонента A являются активные оксиды металла, а каталитический компонент B представляет собой одно или оба из цеолита ZSM-5 и модифицированного металлом, выбранного из Zn, Ga, Sn, Mn, Ag, Zr цеолита ZSM-5. Активный оксид металла представляет собой ...

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 ...

СПОСОБ ПОЛУЧЕНИЯ АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ

Предложен способ получения ароматических углеводородов, включающий пропускание метанола и монооксида углерода через реактор, нагруженный катализатором на основе кислотного молекулярного сита ZSM-5, не содержащим металлическую добавку, с получением ароматических углеводородов при следующих условиях реакции: температура реакции составляет от 350 до 550°С, давление реакции составляет от 0,5 до 10,0 МПа и объемная скорость метанола на единицу массы составляет от 0,01 до 20 ч, и при этом молярное отношение метанола к монооксиду углерода меньше или равно 1:20 и больше или равно 1:100. Технический результат - разработка способа получения ароматических углеводородов из метанола, который обладает преимуществами с точки зрения улучшения селективности при получении ароматических углеводородов и срока службы катализатора без значительного ухудшения рабочих характеристик катализатора после регенерации. 6 з.п. ф-лы, 2 табл., 14 пр.

КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ, ЕЕ ПОЛУЧЕНИЕ И СПОСОБ ПРИМЕНЕНИЯ УКАЗАННОЙ КОМПОЗИЦИИ

СИСТЕМА ДЛЯ ПРОИЗВОДСТВА АРОМАТИЧЕСКОГО СОЕДИНЕНИЯ И СПОСОБ ЕГО ПОЛУЧЕНИЯ

СПОСОБ ПОЛУЧЕНИЯ ПРОПИЛЕНА И АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ И УСТАНОВКА ДЛЯ ИХ ПОЛУЧЕНИЯ

... 1. Способ получения пропилена и ароматических углеводородов, включающий: ! (1) стадию получения пропилена, в которой углеводородное сырье, содержащее 50% по массе или более по меньшей мере одного из С4-12-олефинов контактирует в реакторе для получения пропилена с формованным катализатором А, содержащим первый цеолит, в указанных ниже условиях (i)-(iv) для осуществления реакции каталитической конверсии по меньшей мере одного из С4-12-олефинов, с получением реакционной смеси, содержащей пропилен, реакционная смесь разделяют на фракцию С, содержащую преимущественно водород и C1-3-углеводороды, и фракцию D, содержащую преимущественно по меньшей мере один из С4+-углеводородов, и пропилен выделяют из фракции С: ! (i) с цеолитом, имеющим средний диаметр пор с диаметром пор от 5 до 6,5 Е; ! (ii) по существу не содержащим протонов; ! (iii) содержащим по меньшей мере один металл, выбранный из группы, состоящей из металлов Группы IB Периодической таблицы; и ! (iv) имеющим молярное соотношение SiO2 ...

КАТАЛИЗАТОР ДЛЯ ПИРОЛИЗА СЫРЬЯ

УЛУЧШЕННЫЙ СПОСОБ АЛКИЛИРОВАНИЯ

... 1. Способ получения потока алкилированного ароматического соединения из по меньшей мере одного необработанного потока способного к алкилированию ароматического соединения, находящегося в жидкой фазе и содержащего каталитические яды, и потока алкилирующего агента, причем указанный необработанный поток способного к алкилированию ароматического соединения обрабатывают с целью снижения содержания каталитических ядов, способ включает следующие стадии:(а) контактирование указанного жидкофазного необработанного потока способного к алкилированию ароматического соединения, содержащего указанные каталитические яды, и потока алкилирующего агента с обрабатывающей композицией в зоне обработки, отдельной от реакционной зоны алкилирования, в условиях обработки с целью удаления по меньшей мере части указанных каталитических ядов и алкилирования по меньшей мере части указанного способного к алкилированию ароматического соединения с получением обработанного отходящего потока, который включает обработанное ...

КОМПОЗИЦИЯ КАТАЛИЗАТОРА

СПОСОБ РЕЦИРКУЛЯЦИИ ОЛИГОМЕРИЗАТА НА ОЛИГОМЕРИЗАЦИЮ

СПОСОБ И СИСТЕМА КОНВЕРСИИ МЕТАНОЛА В ЛЕГКИЙ ОЛЕФИН, БЕНЗИН И ДИСТИЛЛЯТ

... 1. Способ получения очищенного углеводорода, включающий:(а) обеспечение сырья, содержащего метанол, диметиловый эфир или их смесь;(б) приведение сырья в контакт с катализатором конверсии метанола в подходящих условиях с получением промежуточной композиции, содержащей олефины, имеющие по меньшей мере два атома углерода;(в) подачу промежуточной композиции к катализатору олигомеризации в подходящих условиях с получением компонентов с пределами температур кипения бензина и компонентов с пределами температур кипения дистиллята; и(г) разделение компонентов с пределами температур кипения бензина и компонентов с пределами температур кипения дистиллята.2. Способ по п.1, дополнительно включающий рециклизацию части выделенных компонентов с пределами температур кипения бензина, содержащих С олефины, в сырье для приведения в контакт с катализатором конверсии метанола с получением C разветвленных парафинов и С ароматических соединений.3. Способ по п.1, в котором рециклизация части выделенных компонентов ...

КАТАЛИЗАТОР НА ОСНОВЕ ZSM-5

Katalysator und Verfahren zur Herstellung von monozyklischen Aromaten

PROCESS FOR THE PRODUCTION OF HARD FRACTURE-RESISTANT CATALYSTS FROM ZEOLITE POWDER

Verfahren zur Qualitätserhöhung von Leichtolefinströmen.

UMWANDLUNG EINES NIEDRIGEN ALKANS.

Verfahren und Anlage zur Herstellung von Olefinen aus Oxygenaten

Verfahren zur Herstellung von Olefinen aus Oxygenaten, umfassend die folgenden Schritte:(i) heterogen-katalysierte Umsetzung von wenigstens einem Oxygenat zu einem flüssige und gasförmige organische Verbindungen und Wasser enthaltenden Gesamtstrom und(ii) Auftrennung des Gesamtstroms in einer ersten Trenneinrichtung in eine zu wenigstens 90 Vol.-% die gasförmigen organischen Verbindungen des Gesamtstroms enthaltende Fraktion, in eine zu wenigstens 90 Gew.-% die flüssigen organischen Verbindungen des Gesamtstroms enthaltende Fraktion und in eine zu wenigstens 90 Gew.-% das Wasser des Gesamtstroms enthaltende Fraktion,iii) Auftrennen der zu wenigstens 90 Vol.-% die gasförmigen organischen Verbindungen des Gesamtstroms enthaltenden Fraktion in einer zweiten Trenneinrichtung in eine C-Verbindungen und Wasser enthaltende Fraktion und eine C-Verbindungen und Oxygenate enthaltende Fraktion,iv) Trocknen der die C-Verbindungen und Wasser enthaltenden Fraktion in einer dritten Trennvorrichtung, so ...

Verfahren zur Herstellung aromatischer Kohlenwasserstoffe

Ein Verfahren zur Herstellung aromatischer Kohlenwasserstoffe umfasst die Schritte: Einleiten eines Eduktgases, welches C1- bis C4-Kohlenwasserstoffe umfasst, in einen Reaktor; Kontaktieren des Eduktgases mit einem Katalysator, wobei ein Produktgas erhalten wird, welches aromatische Kohlenwasserstoffe, Wasserstoff und nicht umgesetzte C1- bis C4-Kohlenwasserstoffe umfasst; Abtrennen der aromatischen Kohlenwasserstoffe von dem Produktgas, wobei ein Abgas erhalten wird, welches Wasserstoff und nicht umgesetzte C1- bis C4-Kohlenwasserstoffe umfasst. Das Kontaktieren des Eduktgases mit einem Katalysator geschieht in einem Reaktor, welcher zumindest teilweise elektrisch beheizt wird und zumindest ein Teil des Abgases wird vorzugsweise in einer Verbrennungsmaschine eines Generators unter Erzeugung elektrischer Energie verbrannt. Die Erfindung betrifft weiterhin einen Reaktor zur Herstellung aromatischer Kohlenwasserstoffe und ein System zur gekoppelten Herstellung von aromatischen Kohlenwasserstoffen ...

Katalysator auf der Basis von kristallinem Alumosilikat.

PROCESS FOR SELECTIVE DEALKYLATION OF ALKYL-SUBSTITUTED AROMATIC HYDROCARBONS

VERFAHREN ZUR HERSTELLUNG VON HARTEN, BRUCHFESTEN KATALYSATOREN AUS ZEOLITH-PULVER

SELECTIVE DEALUMINATION OF ZEOLITES

Process for producing aromatic compound

Disclosed is a process for producing an aromatic compound by a catalytic reaction using a lower hydro-carbon as a starting material, which process can improve the yield of hydrogen and an aromatic compound and can maintain stable catalytic activity. Molybdenum or a molybdenum compound is supported on a metallosilicate, followed by carbonization treatment to obtain a lower hydrocarbon aromatization catalyst. The catalyst is brought into contact with a reaction gas containing a lower hydrocarbon to produce an aromatic compound. In this case, the temperature is raised to a catalytic reaction temperature while allowing an non-oxidative gas (except for a hydrocarbon gas) to flow into the reaction system. When the temperature reaches the catalytic reaction temperature, the reaction gas is allowed to flow into the reaction system to bring the reaction gas into contact with the catalyst to obtain aromatic compounds such as benzene or naphthalene.

HYDROCARBON CONVERSION

... 1402981 Hydrocarbon conversion MOBIL OIL CORP 18 Jan 1974 [9 Feb 1973] 02372/74 Heading C5E Hydrocarbon conversions are carried out using a catalyst comprising a ZSMÀ5 type zeolite defined by X-ray diffraction pattern having an ultimate particle diameter of 0À005- 0À1 Á as crystallized. The catalyst may contain a hydrogenation/dehydrogenation component such as metals, oxides and sulphates of Groups IIB, VIB, VIIB and/or VIII. Examples describe the transalkylation of benzene and diethylbenzene to give ethylbenzene; the alkylation of benzene with ethylene; the alkylation of benzene with n-heptane or n-octane in the presence of hydrogen; the disproportionation of propylene to ethylene and higher olefins; poor point reduction of a gas oil; and cracking a gas oil with a fluidized catalyst.

CONVERSION OF OXYGENATES TO GASOLINE

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

PRODUCTION OF MIDDLE DISTILLATE RANGE HYDROCARBONS

Lower olefins are upgraded to distillate hydrocarbons especially useful as high quality jet or diesel fuels, by oligomerization over a catalyst comprising a shape selective acid zeolite, such as ZSM-5. Reactor effluent is fractionated to recover a light-middle distillate product and to obtain gasoline and heavy hydrocarbon streams for recycle.

OLIGOMERIZATION OF LIQUID OLEFINS

PROCESS FOR THE CONVERSION OF ALKANOLS INTO ETHYLENE AND GASOLINE

Selective production of olefins

A lower alcohol and/or ether feed is selectively converted to a mixture of light olefins, including ethylene and propylene, by catalytic contact of the feed material with a catalyst comprising one or more zeolites characterized by a silica to alumina mole ratio of at least 12 and a constraint index in the approximate range of 1 to 12. The catalytic conversion is carried out in the presence of bulky heterocyclic organic nitrogen compounds to suppress the formation of mono-nuclear aromatics. The process of this invention is particularly useful in the production of C2-C3 olefins from methanol or dimethyl ether.

ETHYLATION OF AROMATIC COMPOUNDS

Production of alkylated compounds

Continuous process for converting natural gas t liquid hydrocarbons

Continuous process for converting natural gas to liquid hydrocarbons

Zone reactor incorporating reversible hydrogen halide capture and release

Continuous process for converting natural gas t liquid hydrocarbons

Continuous process for converting natural gas to liquid hydrocarbons

Continuous process for converting natural gas to liquid hydrocarbons.

Continuous process for converting natural gas to liquid hydrocarbons

Continuous process for converting natural gas t liquid hydrocarbons

Continuous process for converting natural gas to liquid hydrocarbons

Continuous process for converting natural gas to liquid hydrocarbons.

Continuous process for converting natural gas to liquid hydrocarbons

Zone reactor incorporating reversible hydrogen halide capture and release

Continuous process for converting natural gas to liquid hydrocarbons.

ZEOLITES AND THEIR USE

PRODUCTION OF OLEFINEN

PROCEDURE FOR THE PRODUCTION OF A OLEFINI PRODUCT

REACTOR FOR THE PRODUCTION OF C2BIS C8OLEFINEN FROM ONE OXYGENAT, WATER VAPOUR AND ONE OR MORE HYDROCARBONS CONTAINING MATERIAL FLOW

FINECRYSTALLINE ZSM-5 ZEOLITE AND ITS APPLICATION

POROUS INORGANIC MACRO STRUCTURES AND PROCEDURES FOR THE PRODUCTION THE SAME

PROCEDURE FOR THE CATALYTIC CONVERSION OF OLEFINEN

PROCEDURE FOR THE CATALYTIC CONVERSION OF HYDROCARBONS USING SYNTHETIC CRYSTALLINE ALUMOSILICATE.

PROCEDURE AND PLANT FOR THE OLIGOMERISIERUNG OF OLEFINEN

PROCEDURE FOR THE CLEANING OF MIDDLE OLEFINEN

PROCEDURE FOR THE PRODUCTION OF DIMEREN AND OLIGOMEREN OF OLEFINEN

CATALYTIC CONVERSION OF AROMATIC HYDROCARBONS

HEREBY AND THEREFROM

DIRECT CATALYTIC ALKYLATION OF MONONUCLEAR AROMATICS WITH LOWER ALKANES

CATALYTIC CONVERSION OF C3ALIPHATICS TO HIGHER HYDROCARBONS

CONVERTING OLEFINS TO LUBRICANTS AND/OR HEAVY DISTILLATES

MULTISTAGE OLIGOMERISATION OF OLEFINS

Zone reactor incorporating reversible hydrogen halide capture and release

Process for olefin production

Catalyst for propylene production, method for producing same, and method for producing propylene

Disclosed is a catalyst for propylene production, which is used for the purpose of producing propylene from one or more materials selected from the group consisting of methanol, dimethyl ether and olefins having 4-8 carbon atoms. The catalyst for propylene production is characterized in that: the catalyst is composed of a binder-less crystalline aluminosilicate molded body having a silicon/aluminum atomic ratio of 500-10,000; and the crystalline aluminosilicate contains an MFI crystal structure and/or an MEL crystal structure. With the use of this catalyst for propylene production, production amounts of aromatic components and paraffin components such as ethylene and propane are reduced, while achieving excellent propylene yield, propylene/propane ratio and catalyst life.

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.

TITANIUM-CONTAINING ZEOLITES

LOWER OLEFINS TO LIQUID HYDROCARBONS

Process for reducing the benzene content gasoline

A process is described for alkylating benzene contained in a refinery gasoline stream, in which the refinery gasoline stream is contacted with an alkylating agent comprising one or more C2 to C5 olefins in an alkylation reaction zone under alkylation conditions to produce an alkylated effluent. The alkylation reaction zone comprises at least a first alkylation reaction stage and a second alkylation reaction stage and a portion of said alkylating agent is fed to each of said first and second alkylation reaction stages so that, although the molar ratio of alkylatable aromatic to alkylating agent in the total feed to the alkylation reaction zone is less than 1, the molar ratio of alkylatable aromatic to alkylating agent at the inlet of each of the first and second alkylation reaction stages is at least 1.0..

Process for preparing ethylene and/or propylene

The present invention provides a process for preparing ethylene and/or propylene, wherein oxygenates and olefins are converted to ethylene and/or propylene over a zeolite-comprising catalyst, comprising the steps of: a) reacting in a first reactor an oxygenate feed over the zeolite-comprising catalyst at a temperature in the range of from 350 to 1000 °C and retrieving from the first reactor a first reactor effluent stream comprising gaseous products, including ethylene and/or propylene, and zeolite-comprising catalyst; b) reacting in a second reactor an olefin feed over the zeolite-comprising catalyst at a temperature in the range of from 500 to 700 °C and retrieving from the second reactor a second reactor effluent stream comprising gaseous products, including ethylene and/or propylene, and zeolite-comprising catalyst; c) providing the first and second reactor effluent stream to one or more gas/solid separators to retrieve zeolite-comprising catalyst from the first and second reactor effluent ...

Production of xylenes by methylation of aromatic compounds

The inventive method is directed to the production of xylenes by methylation of aromatic compounds with methanol. The process uses fixed bed reactors, operates at lower pressure, and without the need for hydrogen or other gas recycle.

REFORMING HYDROCARBONS

Meta-xylene production process

PROCESS FOR CONVERTING ALCOHOLS/ETHERS INTO OLEFINS USING STEAMED ZEOLITE CATALYSTS

Method of making dimethylnaphtalenes

ZEOLITE CATALYST AND PRODUCTION OF AROMATIC HYDROCARBONS

PROCESS FOR CONVERTING LIGHT OLEFINS INTO HEAVIER HYDROCARBONS

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.

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.

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.

Pre-carburized molybdenum-modified zeolite catalyst and use thereof for the aromatization of lower alkanes

The present invention relates to a method for producing a zeolite catalyst useful for aromatization of a lower alkane, a zeolite catalyst useful for aromatization of a lower alkane obtainable by said method and a process for aromatization of a lower alkane using the zeolite catalyst of the present invention.

Conversion of methylamine to olefin or mixture of olefins

Convert a methylamine (e.g. monomethylamine, dimethylamine and trimethylamine) to a mixture of olefins (e.g. ethylene, propylene and butylene) by placing the methylamine, optionally in a mixture with at least one of ammonia and an inert diluent, in contact with a microporous acidic silicoaluminophosphate catalyst or a microporous aluminosilicate catalyst.

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.

Process for the preparation of a catalyst support

Process for preparing a catalyst support which process comprises a) mixing pentasil zeolite having a bulk silica to alumina molar ratio in the range of from 20 to 150 with water, a silica source and an alkali metal salt, b) extruding the mixture obtained in step (a), c) drying and calcining the extrudates obtained in step (b), d) subjecting the calcined extrudates obtained in step (c) to ion exchange to reduce the alkali metal content, and e) drying the extrudates obtained in step (d); process for preparing a catalyst by furthermore impregnating such support with platinum in an amount in the range of from 0.001 to 0.1 wt % and tin in an amount in the range of from 0.01 to 0.5 wt %, each on the basis of total catalyst; ethylbenzene dealkylation catalyst obtainable thereby and a process for dealkylation of ethylbenzene which process comprises contacting feedstock containing ethylbenzene with such catalyst.

Silica composite, method for producing the same, and method for producing propylene using the silica composite

The present invention provides a method for producing a silica composite by the steps of: preparing a raw material mixture containing silica and zeolite; drying the raw material mixture to obtain a dried product; and calcining the dried product, wherein the method comprising the step of allowing the raw material mixture to contain phosphoric acid and/or phosphate or bringing a solution of phosphoric acid and/or phosphate into contact with the zeolite and/or the dried product, or a combination thereof to thereby adjust a phosphorus content in the silica composite to 0.01 to 1.0% by mass based on the total mass of the silica composite.

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

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

Catalyst for producing monocyclic aromatic hydrocarbon and production method of monocyclic aromatic hydrocarbon

The catalyst for producing aromatic hydrocarbon is for producing monocyclic aromatic hydrocarbon having 6 to 8 carbon number from oil feedstock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower and contains crystalline aluminosilicate and phosphorus. A molar ratio (P/Al ratio) between phosphorus contained in the crystalline aluminosilicate and aluminum of the crystalline aluminosilicate is from 0.1 to 1.0. The production method of monocyclic aromatic hydrocarbon is a method of bringing oil feedstock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower into contact with the catalyst for producing monocyclic aromatic hydrocarbon.

Process for conversion of lower aliphatic ethers to aromatics and lower olefins

The invention relates to a process for converting a feed stream consisting of reactive components and an optional feed diluent to a product stream comprising aromatic hydrocarbons and C2-C3 olefins, wherein the reactive components comprise at least 90 vol % of an aliphatic ether selected from the group consisting of methyl tertiary butyl ether and ethyl tertiary butyl ether, the process comprising the step of contacting the feed stream with a catalyst composition comprising a zeolite catalyst, wherein the zeolite catalyst is a zeolite modified by Ga and an element M1 selected from the group consisting of Zn, Cd and Cu.

Process for making isooctenes from aqueous isobutanol

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

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 Ethylbenzene Conversion in a Xylene Isomerization Process

The present invention relates to a method for converting a feed mixture comprising an aromatic C8 mixture of xylenes and ethylbenzene in which the para-xylene content of the xylene portion of the feed is less than equilibrium to produce a product mixture of reduced ethylbenzene content and a greater amount of para-xylene, which method comprises contacting the feed mixture at conversion conditions with a first catalyst having activity for the conversion of ethylbenzene, and with a second catalyst having activity for the isomerization of a xylene.

ZEOLITIC 3D SCAFFOLDS WITH TAILORED SURFACE TOPOGRAPHY FOR METHANOL CONVERSION WITH LIGHT OLEFINS SELECTIVITY

The present disclosure relates to 3D printed zeolite scaffolds. The zeolite scaffolds can be used as a catalyst for methanol to olefin (MTO) conversion and hydrocarbon cracking processes. 1. A zeolite coated monolith article comprising an uncoated monolithic support structure including walls having a honeycomb structure comprising ammonia-ZSM-5 powder (SiO/AlO) and bentonite clay; and a porous coating disposed directly upon the uncoated monolithic support structure.2. The zeolite coated monolith article of claim 1 , further comprises an additional component selected from the group consisting of amorphous silica claim 1 , a plasticizing binder claim 1 , a metal dopant claim 1 , and combinations thereof disposed within the uncoated monolithic support structure.3. The zeolite coated monolith article of claim 2 , wherein the metal dopant is selected from the group consisting of Zn claim 2 , Ce claim 2 , Cr claim 2 , Mg claim 2 , Cu claim 2 , La claim 2 , Ga claim 2 , Y claim 2 , and combinations thereof.4. The zeolite coated monolith article of claim 1 , wherein the porous coating comprises SAPO-34.5. The zeolite coated monolith article of claim 1 , wherein the zeolite coated monolith has a wall thickness of about 0.2 mm to about 0.9 mm.6. The zeolite coated monolith article of claim 1 , wherein the zeolite coated monolith has a square channel length of about 0.2 mm to about 1.6 mm.7. The zeolite coated monolith article of claim 1 , wherein the zeolite coated monolith has a total pore volume of about 0.2 cm/g to about 0.95 cm/g.8. The zeolite coated monolith article of claim 1 , wherein the zeolite coated monolith has a mesoporosity of about 0.1 cm/g to about 0.95 cm/g.9. A process for converting methanol to one or more light olefins (MTO) claim 1 , the process comprising contacting methanol claim 1 , under deoxygenation conditions claim 1 , with a catalyst comprising a zeolite monolith claim 1 ,{'sub': 2', '2', '3, 'wherein the zeolite monolith comprises an uncoated ...

Process to Make Olefins from Isobutanol

A process for the conversion of an alcohol mixture to make propylene may include introducing into a reactor a stream that includes the alcohol mixture. The alcohol mixture may include 20 to 100 weight percent isobutanol. The process may include contacting the stream with a single catalyst at a temperature above 450° C. in the reactor at conditions effective to dehydrate the isobutanol, forming C olefins, and to catalytically crack the C olefins. The single catalyst may be an acid catalyst adapted to cause both the dehydration and the catalytic cracking. The process may include recovering from the reactor an effluent that includes ethylene, propylene, water, and various hydrocarbons. The process may include fractionating the effluent to produce an ethylene stream, a propylene stream, a fraction of hydrocarbons having 4 carbon atoms or more, and water. 119-. (canceled)20. A process for the conversion of an alcohol mixture comprising about 20 to 100 weight percent isobutanol to make essentially propylene , comprising:a) introducing in a reactor a stream comprising the alcohol mixture, optionally water, optionally an inert component,{'sup': +', '+, 'b) contacting said stream with a single catalyst at a temperature above 450° C. in said reactor at conditions effective to dehydrate at least a part of the isobutanol and other alcohols, if any, forming C4 olefins, and to catalytically crack the C4 olefins, wherein the single catalyst is an acid catalyst adapted to cause both the dehydration and the catalytic cracking,'}c) recovering from said reactor an effluent comprising: ethylene, propylene, water, optionally unconverted alcohols of the alcohol mixture, various hydrocarbons, and the optional inert component of step a),d) fractionating said effluent of step c) to produce at least an ethylene stream, a propylene stream, a fraction consisting essentially of hydrocarbons having 4 carbon atoms or more, water and the optional inert component of step a), optionally recycling ...

Systems and methods for producing propylene

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

Process and catalysts for the production of diesel and gasoline additives from glycerol

A method of producing one or more glycerol ethers, the method comprising contacting glycerol and tertiary butanol (TBA) in the presence of an acidic catalyst to produce one or more glycerol ethers selected from mono-tert butyl glycerol ethers, di-tert butyl glycerol ethers, tri-tert butyl glycerol ethers, or a combination thereof; separating water and a stream comprising isobutylene, unreacted TBA, or a combination thereof from the one or more glycerol ethers; and recycling at least a portion of the stream comprising isobutylene, unreacted TBA, or a combination thereof to the contacting. Also disclosed is a process of co-producing isooctene, wherein the process involves contacting glycerol and tertiary butanol in the presence of a dehydrating catalyst and dimerizing/oligomerizing the dehydrated products in the presence of an oligomerizing catalyst to form isooctene, a precursor of isooctane and isomers thereof.

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 ...

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 ...

HYDROGEN REJECTION IN METHANOL TO HYDROCARBON PROCESS

The present application relates to a process for production of hydrocarbons comprising the steps of —converting a feed stream comprising alcohols, ethers or mixtures hereof over a metal-containing zeolite based catalyst, active in dehydrogenation of hydrocarbons, in a conversion step thereby obtaining a conversion effluent, —separating said effluent to obtain an aqueous process condensate stream, a liquid hydrocarbon stream and a gaseous stream, —removing part of the hydrogen formed in the conversion step, and recycling at least part of the gaseous and/or liquid hydrocarbon stream to the conversion step. 1. A process for production of hydrocarbons comprising the steps ofconverting a feed stream comprising alcohols, ethers or mixtures hereof over a metal-containing zeolite based catalyst, active in dehydrogenation of hydrocarbons, in a conversion step thereby obtaining a conversion effluent,separating said effluent to obtain an aqueous process condensate stream, a liquid hydrocarbon stream and a gaseous stream,removing part of the hydrogen formed in the conversion step,{'sub': '2', 'obtaining an at least partly Hdepleted recycle stream,'}{'sub': '2', 'recycling at least part of the at least partly Hdepleted recycle stream, the gaseous and/or liquid hydrocarbon streams to the conversion step.'}2. A process according to wherein hydrogen is removed by purging at least part of the gaseous recycle stream.3. A process according to claim 1 , wherein the at least partially Hdepleted recycle stream is obtained from the gaseous stream by passing the gaseous stream to a hydrogen permselective membrane.4. A process according to claim 1 , wherein the at least partially Hdepleted recycle stream is obtained from the gaseous stream by passing said gaseous phase claim 1 , after admixture with a predetermined amount of dioxygen claim 1 , to a catalytic oxidation step where hydrogen is reacted with said predetermined amount of oxygen to form water and recycling said reacted stream ...

Catalyst used in the production of ethylene and propylene from methanol and/or dimethyl ether, method for preparing the same and method for using the same

The application provides a catalyst for producing ethylene and propylene from methanol and/or dimethyl ether, and a preparation and application thereof. In the present application, a molecular sieve catalyst co-modified by rare earth metals and silanization is utilized. First, the material containing methanol and/or dimethyl ether reacts on the catalyst to generate hydrocarbons. The hydrocarbons are separated into a C 1 -C 5 component and a C 6 + component. Then the C 6 + component is recycled to the feeding port and fed into the reactor after mixing with methanol and/or dimethyl ether. The above steps are repeated, to finally generate C 1 -C 5 products, in which the selectivity for ethylene and propylene can reach more than 90 wt % in the C 1 -C 5 component, so that the maximal yield can be achieved in the production of ethylene and propylene from methanol and/or dimethyl ether.

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 ...

Conversion of mixtures of c2-c8 olefins to jet fuel and/or diesel fuel in high yield from bio-based alcohols

The present disclosure provides methods and materials for oligomerization of lower olefins (e.g., C 2 -C 8 ) to transportations fuels including diesel and/or jet fuel. The oligomerization employs, in certain embodiments, tungstated zirconium catalysts. Surprisingly, the oligomerizations proceed smoothly in high yields and exhibit little to no sensitivity to the presence of significant amounts of oxygenates (e.g., water, lower alcohols such as C 2 -C 8 alcohols) in the feed stream. Accordingly, the present disclosure is uniquely suited to the production of fuels derived from bio-based alcohols, wherein olefins produced from such bio-based alcohols typically contain high levels of oxygenates.

METHOD OF TREATING BUTENE TO FORM PROPYLENE/ETHYLENE MIXTURE

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

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

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

Treatment of Aromatic Alkylation Feedstock

In a process and system for treatment of feed stocks comprising alkylating agent and metal salts, the metal salts are removed from the feedstock by an efficient combination of separations processes. The processes may take place in one or more stages, each stage taking place in one or more vessels. Such treatment processes may remove 99.9% or more of metal salts from a feedstock, while recovering 99.9% or more of the alkylating agent from the feedstock for use in an alkylation reaction, especially of aromatics such as toluene and benzene. Preferred alkylating agents include methanol and mixtures of carbon monoxide and hydrogen, for methylation of toluene and/or benzene. The methylation proceeds over an aluminosilicate catalyst and preferably yields para-xylene with 75% or greater selectivity.

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.

Use of Light Gas By-Products in the Production of Paraxylene by the Methylation of Toluene and or Benzene

A process for producing paraxylene by the catalytic alkylation of benzene and/or toluene with methanol, which produces a para-rich mixture of xylene isomers, together with water and some light organic by-products, particularly dimethyl ether and C− olefins. The off-gas stream, containing the C olefins, may be recycled back to the reaction to be co-injected with methanol to reduce the methanol self-decomposition and the reaction of methanol to olefins or to fluidize catalyst particles recovered by a reactor cyclone. By using recycled off-gas rather than water or steam, the deleterious effects of water and/or steam on the catalyst aging and activity rates and the size of downstream equipment necessary to recover olefin by-products may be reduced. 1. A process for the alkylation of toluene and/or benzene to produce paraxylene (PX) comprising contact of said toluene and/or benzene with an alkylating agent selected from methanol , dimethyl ether , and mixtures thereof , in the presence of an alkylation catalyst in a fluidized bed alkylation reactor under conditions effective to produce an alkylation effluent comprising PX and olefins , wherein the alkylation effluent is separated into a stream comprising PX and a light gas stream comprising olefins , the improvement comprising recycling at least a portion of the light gas stream , including olefins , to the alkylation reactor for injection with alkylating agent , fluidizing particles of the alkylation catalyst recovered from the alkylation effluent , or both.2. The process of claim 1 , wherein the light gas stream further comprises oxygenates claim 1 , unreacted alkylating agent claim 1 , and contaminants claim 1 , and is treated to remove at least one of the oxygenates claim 1 , alkylating agent claim 1 , and contaminants prior to recycling the light gas stream to the alkylation reactor.3. The process of claim 1 , wherein the alkylating agent is methanol.4. The process of claim 3 , wherein the methanol and recycled ...

METHODS FOR MAKING LIGHT OLEFINS FROM DIFFERENT FEED STREAMS

According to one or more embodiments of the present disclosure, chemical streams may be processed by a method which may comprise operating a first chemical process, stopping the first chemical process and removing the first catalyst from the reactor, and operating a second chemical process. The reaction of the first chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The reaction of the second chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The first reaction and the second reaction may be different types of reactions. 2. The method of claim 1 , wherein the first product stream and the second product stream comprise one or more of ethylene claim 1 , propylene claim 1 , or butene.3. The method of claim 1 , wherein the first reaction or the second reaction is a dehydrogenation reaction claim 1 , and the first catalyst or the second catalyst comprises gallium claim 1 , platinum claim 1 , or both.4. The method of claim 1 , wherein:the first reaction or the second reaction is a dehydrogenation reaction; andthe first feed stream or the second feed stream comprises one or more of ethane, propane, n-butane, and i-butane.5. The method of claim 1 , wherein the first reaction or the second reaction is a cracking reaction claim 1 , and the first catalyst or the second catalyst comprises one or more zeolites.6. The method of claim 1 , wherein:the first reaction or the second reaction is a cracking reaction; andthe first feed stream or the second feed stream comprises one or more of naphtha, n-butane, or i-butane.7. The method of claim 1 , wherein the first reaction or the second reaction is a dehydration reaction claim 1 , and the first catalyst or second catalyst comprises one or more acid catalysts.8. The method of claim 1 , wherein:the first reaction or the second reaction is a dehydration reaction;the first feed ...

Process and Catalyst for Methane Conversion to Aromatics

A process and catalyst for use therein for the production of aromatics via the oxidative coupling of methane and methane co-aromatization with higher hydrocarbons in a single reaction stage. First, methane is partially converted to ethane and ethylene on an OCM catalyst component, and the OCM intermediate mixture containing methane, ethane and ethylene is subsequently converted into aromatics on an aromatization catalyst component. The reaction may be conducted at 550-850° C. and at about 50 psig. The claimed process and catalyst used therein achieves high methane conversion at lower temperatures (less than 800° C.), higher methane conversion into the aromatic products and significant reductions in production cost when compared to the traditional two (or more) step processes. 1. A process for producing aromatics , the process comprising:a. providing a feed comprising methane and an oxidant;b. contacting the feed with a catalyst comprising an oxidative coupling of methane (“OCM”) component and an aromatization component under conditions, including a temperature of about 600-800° C., effective to convert at least part of the methane in the feed to a product comprising at least 7 wt. % of aromatics, based on the weight of the product, wherein the OCM catalyst component and aromatization catalyst component are contained within a single reactor, wherein the OCM catalyst component comprises at least one alkaline/rare earth metal oxide, wherein the aromatization catalyst component comprises at least one molecular sieve and at least one dehydrogenation component; andc. separating at least part of the aromatics from the product.2. The process of claim 1 , wherein the OCM catalyst component and the aromatization catalyst component are physically mixed within the reactor.3. The process of claim 1 , wherein multiple layers of OCM catalyst component are alternated with multiple layers of aromatization catalyst component claim 1 , forming a stacked bed of catalyst within the ...

OLIGOMERIZATION OF ETHYLENE TO LIQUID TRANSPORTATION FUELS WITH POST SYNTHESIS TREATED ZSM-5 CATALYST

A process for post synthesis treatment of ZSM-5 catalyst for converting ethylene to liquid fuel products providing substantially improved catalyst life. The treatment comprises either a base treatment, an acid treatment or a two-step treatment where one is with an acid and the other is with a base. The base treatment is provided by a weak sodium hydroxide such as less than 1 Molar concentration. The acid treatment is stronger acid where, for example, a hydrogen chloride solution at greater than 2 Molar concentration is used. 1. Oligomerizing ethylene to transportation fuel products in a reactor with a fixed bed of ZSM-5 catalyst that is essentially free of catalyst metals other than silica and alumina wherein the ZSM-5 catalyst has been provided with post synthesis two step treatment of an acid wash and a base wash to resist coke formation in the zeolite crystallites and extend catalyst life wherein the oligomerizing is conducted at a pressure between 0 psig and 800 psig , a temperature of between 260° C. and 420° C. , and a gas hourly space velocity of between 1000 and 5000 inverse hours and wherein at least 85% of the ethylene is converted.2. The process according to wherein the post synthesis treatment of the catalyst comprises catalyst a base treatment with sodium hydroxide and an acid treatment of hydrogen chloride.3. The process according to wherein the base treatment of sodium hydroxide is at between about 0.001 and about 0.5 Molar concentration.4. The process according to wherein the base treatment of sodium hydroxide is at between about 0.005 and about 0.25 Molar concentration.5. The process according to wherein the base treatment of sodium hydroxide is at between about 0.0075 and about 0.15 Molar concentration.6. The process according to wherein the acid treatment of hydrogen chloride is at between about 1 and 10 Molar concentration.7. The process according to wherein the acid treatment of hydrogen chloride is at between about 2 and 7 Molar concentration.8 ...

OLIGOMERIZATION OF ETHYLENE TO LIQUID TRANSPORTATION FUELS WITH POST SYNTHESIS TREATED ZSM-5 CATALYST

A process for post synthesis treatment of ZSM-5 catalyst for converting ethylene to liquid fuel products providing substantially improved catalyst life. The treatment comprises either a base treatment, an acid treatment or a two-step treatment where one is with an acid and the other is with a base. The base treatment is provided by a weak sodium hydroxide such as less than 1 Molar concentration. The acid treatment is stronger acid where, for example, a hydrogen chloride solution at greater than 2 Molar concentration is used. 1. Oligomerizing ethylene to transportation fuel products in a reactor with a fixed bed of ZSM-5 catalyst that is essentially free of catalyst metals other than silica and alumina wherein the ZSM-5 catalyst has been provided with post synthesis acid treatment to resist coke formation in the zeolite crystallites and extend catalyst life wherein the oligomerizing is conducted at a pressure between 0 psig and 800 psig , a temperature of between 260° C. and 420° C. , and a gas hourly space velocity of between 1000 and 5000 inverse hours wherein at least 85% of the ethylene is converted.2. The process according to wherein the post synthesis treatment of the catalyst comprises catalyst an acid treatment with hydrogen chloride.3. The process according to wherein the acid treatment is a hydrogen chloride solution at between about 1 and 10 Molar concentration.4. The process according to wherein the acid treatment is between about 2 and 7 Molar concentration.5. The process according to wherein the acid treatment is between about 3 and 5 Molar concentration.6. The process according to wherein the post synthesis treatment of the catalyst further comprises the steps of drying catalyst and calcining the catalyst after the acid treatment.7. The process according to wherein the post synthesis treatment of the catalyst further comprises the steps of drying catalyst at a temperature above 105° C. and calcining the catalyst after the acid treatment at a ...

OLIGOMERIZATION OF ETHYLENE TO LIQUID TRANSPORTATION FUELS WITH POST SYNTHESIS TREATED ZSM-5 CATALYST

A process for post synthesis treatment of ZSM-5 catalyst for converting ethylene to liquid fuel products providing substantially improved catalyst life. The treatment comprises either a base treatment, an acid treatment or a two-step treatment where one is with an acid and the other is with a base. The base treatment is provided by a weak sodium hydroxide such as less than 1 Molar concentration. The acid treatment is stronger acid where, for example, a hydrogen chloride solution at greater than 2 Molar concentration is used. 1. Oligomerizing ethylene to transportation fuel products in a reactor with a fixed bed of ZSM-5 catalyst that is essentially free of catalyst metals other than silica and alumina wherein the ZSM-5 catalyst has been provided with post synthesis treatment of a base wash to resist coke formation in the zeolite crystallites and extend catalyst life wherein the oligomerizing is conducted at a pressure between 0 psig and 800 psig , a temperature of between 260° C. and 420° C. , and a gas hourly space velocity of between 1000 and 5000 inverse hours and wherein at least 85% of the ethylene is converted.2. The process according to wherein the post synthesis treatment of the catalyst comprises catalyst a base treatment with sodium hydroxide.3. The process according to wherein the base treatment is with a solution of sodium hydroxide at between about 0.001 and about 0.5 Molar concentration.4. The process according to wherein the base treatment is with a solution of sodium hydroxide at between about 0.005 and about 0.25 Molar concentration.5. The process according to wherein the base treatment is with a solution of sodium hydroxide at between about 0.0075 and about 0.15 Molar concentration.6. The process according to wherein the post synthesis treatment of the catalyst further comprises the steps of drying catalyst and calcining the catalyst after the base-acid treatment.7. The process according to wherein the post synthesis treatment of the catalyst ...

Process for Xylenes Isomerization

A process for the isomerization of a para-xylene depleted, meta-xylene rich stream under at least partially liquid phase conditions using ZSM-23 with an external surface area of at least 75 m/g (indicating a small crystallite size), and a SiO/AlOratio between 15 and 75 that produces a higher than equilibrium amount of para-xylene, i.e., more than about 24 wt % of para-xylene, based on the total amount of xylenes. 1. A process for producing para-xylene comprising contacting a feed stream comprising meta-xylene with a catalyst comprising ZSM-23 having a SiO/AlOratio between 15 and 75 and an external surface area of at least 75 m/g under at least partially liquid phase conditions effective to produce a first isomerized stream comprising para-xylene having a para-xylene content of more than 24 wt % , based on the total amount of xylenes in the first isomerized stream.2. The process of claim 1 , wherein the catalyst comprises ZSM-23 having SiO/AlOratio between 15 and 50 and an external surface area of at least 90 m/g.3. The process of claim 1 , wherein the catalyst is self-bound.4. The process of claim 1 , wherein the feed stream consists essentially of meta-xylene.5. The process of claim 1 , wherein the liquid phase conditions comprise a temperature from 400° F. (204° C.) to 1 claim 1 ,000° F. (538° C.) claim 1 , a pressure of from 0 to 1 claim 1 ,000 psig claim 1 , a weight hourly space velocity (WHSV) of from 0.5 to 100 hr.6. The process of claim 5 , wherein the liquid phase conditions comprise a temperature from 482° F. (250° C.) to 572° F. (300° C.) claim 5 , a pressure from 350 psig (2.41 MPa) to 500 psig (3.45 MPa) claim 5 , and a weight hourly space velocity (WHSV) from 0.5 to 10 hr.7. The process of claim 1 , wherein said feed stream comprising meta-xylene is produced by:{'sub': '8', '(a) providing a Caromatic hydrocarbon mixture comprising para-xylene, ortho-xylene and meta-xylene to an ortho-xylene splitter;'}(b) recovering a first stream comprising para- ...

Production of Xylenes from Syngas

This disclosure relates to the production of xylenes from syngas, in which the syngas is converted to an aromatic product by reaction with a Fischer-Tropsch catalyst and an aromatization catalyst. The Fischer-Tropsch catalyst and aromatization catalyst may be different catalysts or combined into a single catalyst. The aromatic product is then subjected to selective alkylation with methanol and/or carbon monoxide and hydrogen to increase its p-xylene content. 1. A catalyst system for the production of para-xylene comprising:(a) a first catalyst comprising 1 to 50 wt. % Fe, and(b) a second catalyst comprising at least one medium pore size molecular sieve and at least one metal or compound thereof, wherein the metal is selected from Groups 10-14 of the Periodic Table,wherein the first and second catalysts are located within the same reactor bed, andwherein the second catalyst is selectivated by contacting the second catalyst with steam at a temperature of at least 950° C. for about 10 minutes to 10 hours.2. The catalyst system of wherein the first and second catalysts are physically mixed in the same reactor bed.3. The catalyst system of wherein the first and second catalysts are combined into a single multi-functional catalyst.4. The catalyst system of claim 1 , wherein the first catalyst comprises at least one support selected from the group consisting of zinc oxide claim 1 , manganese oxide claim 1 , alumina claim 1 , silica claim 1 , carbon claim 1 , and mixtures thereof.5. The catalyst system of claim 1 , wherein the second catalyst comprises at least one metal or compound thereof claim 1 , wherein the metal is selected from the group consisting of Ga claim 1 , In claim 1 , Zn claim 1 , Cu claim 1 , Re claim 1 , Mo claim 1 , W claim 1 , La claim 1 , Fe claim 1 , Ag claim 1 , Pt claim 1 , and Pd.6. The catalyst system of claim 1 , wherein the metal of the second catalyst is present in an amount of about 0.1 to 10 wt %.7. The catalyst system of claim 1 , wherein the ...

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

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

LOW-ENERGY CONSUMPTION METHOD FOR DEHYDRATING ETHANOL INTO ETHYLENE

A process for dehydrating an ethanol feedstock to give ethylene, includes: 1. A process for dehydrating an ethanol feedstock to give ethylene , comprising:a) a stage for vaporizing a vaporization feedstock comprising said ethanol feedstock in an exchanger by means of a heat exchange with a dehydration effluent resulting from stage c), so as to produce a vaporized feedstock;b) a stage for heating said vaporized feedstock in an exchanger by means of a heat exchange with a thermal fluid, so as to produce a superheated feedstock having a temperature of greater than 400° C. and less than 550° C.;c) a stage for dehydrating said superheated feedstock so as to produce a dehydration effluent, wherein said stage for dehydrating comprises a reaction section comprising at least one multitubular reactor in which the dehydration reaction takes place, said multitubular reactor comprising a plurality of tubes having a length of between 2 and 4 m and a shell, said tubes each comprising at least one fixed bed comprising at least one dehydration catalyst, said superheated feedstock being introduced into said tubes at an inlet temperature of greater than 400° C. and less than 550° C. and at an inlet pressure of between 0.8 and 1.8 MPa,a heat transfer fluid circulating inside said shell at a mass flow rate such that the ratio of the mass flow rate of said heat transfer fluid in the shell relative to the mass flow rate of said superheated feedstock introduced into said tubes is greater than or equal to 10, said heat transfer fluid having a temperature at the inlet into the shell of said multitubular reactor of greater than 430° C. and less than 550° C.;d) a stage for separating the dehydration effluent resulting from stage c) into an effluent comprising ethylene at a pressure of less than 1 MPa and an effluent comprising water;e) a stage for purifiying at least a portion of the effluent comprising water resulting from staged) and the separation of at least one stream of purified water ...

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.

MFI Aluminosilicate Molecular Sieves and Methods for Using Same for Xylene Isomerization

MFI aluminosilicate molecular sieve catalysts are prepared from tetra-functional orthosilicates [e.g., Si(OR)(OR)(OR)(OR), wherein RRRRis each independently a Calkyl or aryl.] as the silicon source. Such catalysts are useful for hydrocarbon conversion reactions including isomerization of xylenes in Caromatics feed stocks to produce p-xylene. Advantageously, it has been found that the MFI aluminosilicate molecular sieve catalysts of the invention are more selective than conventional commercial MFI catalysts, resulting in reduced formation of transmethylation byproducts (Cand Caromatics) while simultaneously providing a high degree of xylene isomerization. 1. A method of increasing the proportion of p-xylene (pX) in a hydrocarbon-containing feed stream comprising xylene isomers , said method comprising:contacting the hydrocarbon-containing feed stream with an isomerization catalyst under conditions suitable to yield a stream enriched in p-xylene with respect to the hydrocarbon-containing feed stream, wherein{'sub': 1', '2', '3', '4', '1', '2', '3', '4', '1-10, 'the isomerization catalyst comprises a WI aluminosilicate molecular sieve prepared using a silicon source comprising a compound of the formula, Si(OR)(OR)(OR)(OR), wherein RRRRis each independently a Calkyl or aryl.'}2. The method of claim 1 , further comprising recovering byproducts from the pX enriched stream.3. The method of claim 2 , wherein the byproducts contain 1.5 wt. % or less net toluene byproduct.4. The method of claim 2 , wherein the byproducts contain 3.5 wt. % or less net C-byproducts.5. The method of claim 1 , wherein the pX enriched stream contains less than 0.7 wt. % net trimethylbenzene byproduct.6. The method of claim 1 , wherein the pX enriched stream contains less than 1.0 wt % net toluene.7. The method of claim 1 , wherein the pX enriched stream contains less than 0.5 wt. % net trimethylbenzene byproduct.8. A method of increasing the proportion of p-xylene (pX) in a hydrocarbon-containing ...

Methods and systems for processing lignin during hydrothermal digestion of cellulosic biomass solids

Digestion of cellulosic biomass solids may be complicated by release of lignin therefrom. Methods for digesting cellulosic biomass solids may comprise: providing cellulosic biomass solids in a digestion solvent; at least partially converting the cellulosic biomass solids into a phenolics liquid phase comprising lignin, an aqueous phase comprising an alcoholic component derived from the cellulosic biomass solids, and an optional light organics phase; and separating the phenolics liquid phase from the aqueous phase, at least partially depolymerizing the lignin in the phenolics liquid phase, wherein at least partially depolymerizing the lignin generates hydrocarbons.

Process for preparing a hierarchical zeolite catalyst for aromatization of C5-C9 alkane

A process for preparing a hierarchical zeolite catalyst for aromatization of C5-C9 alkane that provides high conversion percentage of precursor to yields and high aromatics selectivity, wherein said process comprises the following steps: 1. A process for preparing a hierarchical zeolite catalyst for aromatization of C5-C9 alkane , wherein said process comprises the following steps:(a) preparing a solution containing alumina compound, silica compound, and soft template;(b) subjecting the mixture obtained from step (a) to hydrothermal process at determined time and temperature to form said mixture into the hierarchical zeolite;(c) contacting the hierarchical zeolite obtained from step (b) with ammonium salt solution; and(d) contacting the hierarchical zeolite obtained from step (c) with gallium salt solution;characterized in that the soft template in step (a) is a quaternary phosphonium salt in which the mole ratio of the silica compound to the alumina compound in step (a) is in a range of 20 to 120 and the gallium salt in step (d) has gallium to zeolite ratio in a range of 0.5 to 5% by weight.2. The process for preparing according to claim 1 , wherein the quaternary phosphonium salt is tetraalkylphosphonium selected from tetrabutylphosphonium hydroxide and tributyl hexadecyl phosphonium bromide.3. The process for preparing according to claim 2 , wherein the quaternary phosphonium salt is tetrabutylphosphonium hydroxide.4. The process for preparing according to claim 1 , wherein the mole ratio of the silica compound to the alumina compound in step (a) is in the range of 20 to 60.5. The process for preparing according to claim 1 , wherein the gallium salt in step (d) has gallium to zeolite ratio in the range of 0.5 to 1% by weight.6. The process for preparing according to claim 1 , wherein the gallium salt is selected from gallium nitrate claim 1 , gallium chloride claim 1 , gallium bromide claim 1 , gallium hydroxide claim 1 , and gallium acetate.7. The process for ...

Catalyst and method for synthesis of aromatic hydrocarbons through direct conversion of synthesis gas

Synthesis of aromatic hydrocarbons from synthesis gas in a fixed bed or a moving bed reactor loaded with a composite catalyst comprising Catalyst Component A and Catalyst Component B mixed via a mechanical mixing mode, wherein the active ingredient of the Catalyst Component A is active metal oxides; and the Catalyst Component B is one or both of ZSM-5 zeolite and metal modified ZSM-5; the pressure of the synthesis gas is 0.1-6 MPa; the reaction temperature is 300-600° C.; and the space velocity is 500-8000 h−1. The reaction process has a high product yield and selectivity, with the selectivity of aromatics reaching 50-85%, while the selectivity of the methane byproduct is less than 15%.

A Process for Preparing Perhydrofluorene or Alkyl-Substituted Perhydrofluorene

The present invention discloses a process for preparing perhydrofluorene or alkyl-substituted perhydrofluorene, comprising the steps of: (1) reacting a phenolic compound or an aromatic hydrocarbon compound or an aromatic ketone compound or an aromatic ether compound with a benzyl compound to carry out an alkylation reaction in the presence of a first catalyst, thereby to produce substituted or unsubstituted diphenyl methane, wherein the first catalyst is an acidic catalyst; and (2) reacting the substituted or unsubstituted diphenyl methane with hydrogen gas to carry out an hydrogenation reaction or a hydrodeoxygenation reaction, thereby to produce perhydrofluorene or alkyl-substituted perhydrofluorene, wherein the second catalyst is a physical mixture of a metal catalyst and an acidic catalyst or a metal catalyst loaded on an acidic catalyst.

CONVERSION OF SHALE GAS TO AROMATICS

A method for converting shale gas to aromatic hydrocarbons includes passing a feedstock comprising ethane gas and methane gas to an aromatization reactor; converting a portion of the methane gas and ethane gas in the feedstock to liquid aromatic hydrocarbons with a zeolite based catalyst at a temperature of 750 C to 900 C; separating unconverted methane gas from liquid aromatic hydrocarbons; separating unconverted methane gas from the unconverted ethane gas; recycling the separated methane gas to the aromatization reactor; recovering aromatic hydrocarbons in a product stream after separation and removal from the aromatization reactor. Less than or equal to 95% of the ethane is converted to aromatic hydrocarbons. 1. A method for converting shale gas to aromatic hydrocarbons , comprising:passing a feedstock comprising ethane gas and methane gas to an aromatization reactor;converting a portion of the methane gas and ethane gas in the feedstock to liquid aromatic hydrocarbons with a zeolite based catalyst at a temperature of 750° C. to 900° C.;separating unconverted methane gas from liquid aromatic hydrocarbons;separating unconverted methane gas from the unconverted ethane gas;recycling the separated methane gas to the aromatization reactor;recovering aromatic hydrocarbons in a product stream after separation and removal from the aromatization reactor;wherein less than or equal to 95% of the ethane is converted to aromatic hydrocarbons.2. The method of claim 1 , wherein the feedstock is a shale gas feedstock.3. The method of claim 1 , wherein the feedstock further comprises propane claim 1 , butane claim 1 , pentane claim 1 , carbon dioxide claim 1 , oxygen claim 1 , nitrogen claim 1 , hydrogen sulfide claim 1 , or a combination comprising at least one of the foregoing.4. The method of claim 1 , wherein the feedstock comprises 75-85 mol % methane.5. The method of claim 1 , wherein the feedstock comprises 10-25 mol % ethane.6. The method of claim 1 , wherein less than or ...

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 the catalyst composition under conversion conditions effective to dealkylate and transalkylate said C aromatic hydrocarbons to produce said lighter aromatic products comprising benzene, toluene and xylene. The catalyst composition comprises a zeolite, a first metal, and a second metal, and is treated with a source of sulfur and/or a source of steam. 125.-. (canceled)26. A process for conversion of a feedstock comprising Caromatic hydrocarbons to lighter aromatic products , the process comprising the step of contacting said feedstock and optionally hydrogen in the presence of a catalyst composition under conversion conditions effective to dealkylate and transalkylate said Caromatic hydrocarbons to produce said lighter aromatic products comprising benzene , toluene and xylene ,wherein said catalyst composition is treated with a source of sulfur and/or steam and comprises:(i) at least one zeolite selected from the group consisting of zeolite beta, ZSM-4, ZSM-5, ZSM-11, ZSM-12, ZSM-20, ZSM-22, ZSM-23, ZSM-35, ZSM-48, ZSM-50, ZSM-57, ZSM-58, MCM-68, a faujasite zeolite, a mordenite zeolite, a MCM-22 family material, or a mixture thereof,(ii) 0.001 wt. % to 20.0 wt. % of at least one first metal, said first metal being in Group 6 of the Periodic Table, based on the weight of said catalyst composition, and(iii) 0.001 wt. % to 20.0 wt. % of at least one second metal, said second metal being in Group 9 or Group 10 of the Periodic Table, based on the weight of said catalyst composition.27. The process of claim 26 , wherein said catalyst composition is treated with said source of sulfur in one or more steps at temperatures in the range 204° C. (400° F.) up to about 480° C. (900° F.).28. The process of claim 27 , wherein said source of sulfur is one or more of hydrogen sulfide claim ...

Xylene Isomerization Process and Catalyst Therefor

The invention concerns a xylenes isomerization process for the production of equilibrium or near-equilibrium xylenes from a feedstream comprising phenol and/or styrene. 1. A process for the isomerization of a paraxylene-depleted aromatic hydrocarbon feedstream comprising styrene , wherein said isomerization of a paraxylene-depleted feedstream is conducted in the presence of a catalyst comprising HZSM-5 , wherein said HZSM 5 is characterized by an average crystal size of <0.1 micron and a SiO/AlOmolar ratio in the range of about 20-100 , in a reactor at a temperature of less than 295° C. , and a pressure sufficient to maintain the xylenes in liquid phase.24-. (canceled)5. The process of claim 1 , wherein said feedstream is characterized as containing styrene in the amount of 100 ppm or less.6. The process of claim 1 , wherein said feedstream is characterized as containing styrene in the amount of 50 ppm or less.7. The process of claim 1 , wherein said feedstream is characterized as containing styrene in the amount of 20 ppm or less.8. The process of claim 1 , further characterized in that said process is operated in a continuous mode with a feedstream containing low ppm levels of dissolved Hin the range of about 4 to 100 ppm.9. The process of claim 1 , further characterized in that said process is operated in a continuous mode with a feedstream containing low ppm levels of dissolved Hin the range of about 4 to 20 ppm.10. The process of claim 1 , further characterized in that said process is operated in a cyclic mode with an H-free feedstream claim 1 , and further wherein said catalyst is periodically regenerated by a step including contacting said catalyst with an H-containing feedstream claim 1 , wherein said H-free feedstream is characterized as containing less than 4 ppm dissolved Hand said H-containing feedstream is characterized as containing about 4 or more ppm dissolved H.11. The process of claim 1 , wherein said reactor is at a temperature of 260° C. or less. ...

METHOD OF METHYL CYCLOPENTENE PRODUCTION FROM CYCLOHEXENE OVER ZEOLITE-BASED CATALYST STRUCTURE

Selective conversion from cyclohexene to methylcyclopentene can occur via skeletal isomerization reaction under mild temperature and near atmospheric pressure with the existence of a catalyst structure as described herein. The catalyst structure includes a porous zeolite as the support and one or more loaded metals to further modify its acidity and pore structures. Industrially available cyclohexene feedstock can be effectively converted to a high value-added product methylcyclopentene with over 90 wt % conversion and 95 wt % selectivity, which is highly profitable for potential application in the fine chemical industry. 1. A method for producing methylcyclopentene from cyclohexene via skeletal isomerization , the method comprising:reacting cyclohexene within a reactor in the presence of a gas atmosphere and a catalyst structure, wherein the catalyst structure comprises a porous support structure and one or more metals loaded in the porous support structure, the porous support structure comprises an aluminosilicate material, and the one or more metals loaded in the porous support structure is selected from the group consisting of Na, K, Co, Mo, Ag, Ga and Ce.2. The method of claim 1 , wherein the porous support structure includes Co and/or Mo.3. The method of claim 1 , wherein the gas atmosphere comprises a pure gas or a mixture of two or more gases selected from the group consisting of nitrogen claim 1 , helium claim 1 , methane claim 1 , and argon.4. The method of claim 1 , wherein the aluminosilicate material is selected from the group consisting of HZSM-5 type zeolite claim 1 , L-type zeolite claim 1 , HX type zeolite claim 1 , and HY type zeolite.5. The method of claim 1 , wherein each metal loaded in the porous support structure is present in an amount from 0.1 wt % to 20 wt % by weight of the catalyst support structure.6. The method of claim 5 , wherein the one or more metal components is loaded in the porous support structure as one or more salts selected ...

Catalyst and Process for the Production of Para-Xylene

A fluidized bed process for producing para-xylene via toluene and/or benzene methylation with methanol using a dual function catalyst system. A first catalyst accomplishes the toluene and/or benzene methylation and a second catalyst converts the by-products of the methylation reaction or unconverted methylating agent, improves the yields of the desired products, or a combination thereof. The inclusion of the second catalyst can suppress the C1-C5 non-aromatic fraction by over 50% and significantly enhance the formation of aromatics.

PROCESS FOR PRODUCING SHORT-CHAIN OLEFINS FROM OXYGENATES

There is proposed a process for producing short-chain olefins by conversion of oxygenates in a multi-stage fixed-bed reactor (OTO reactor) with reaction zones each operated adiabatically, in which the individual stages or reaction zones are covered with beds of a granular, form-selective zeolite catalyst which previously has been subjected to a steam pretreatment in an external, isothermally or quasi-isothermally operated steam pretreatment reactor. By means of the external steam pretreatment according to the invention, higher lifetimes of the catalyst used are obtained as compared to a steam pretreatment in the OTO reactor. The availability of the OTO reactor for the olefin production is increased. 114-. (canceled)15. A process for producing a hydrocarbon product containing short-chain , low-molecular olefins , comprising ethylene and propylene , the process comprising the steps of:converting an educt mixture comprising steam and oxygenates, under oxygenate conversion conditions to olefins in an oxygenate-to-olefin synthesis reactor (OTO reactor) with several series-connected reaction zones in fluid connection with each other, which are each operated adiabatically and which are filled with a solid, granular, form-selective oxygenate-to-olefin synthesis catalyst (OTO catalyst) on the basis of a zeolite or molecular sieve material,wherein the OTO catalyst is present in the reaction zones as fixed bed or as non-fluidized moving bed,wherein the OTO reactor is charged with the educt mixture and a product stream comprising olefins is discharged from the OTO reactor,subjecting the OTO catalyst, prior to being used in the OTO reactor, to a steam pretreatment, wherein the steam pretreatment is carried out outside the OTO reactor in a steam pretreatment reactor under steam pretreatment conditions.16. The process according to claim 15 , wherein the OTO catalyst comprises a material selected from the group consisting of an alumosilicate zeolite of the pentasil type and a ...

High severity fluidized catalytic cracking systems and processes for producing olefins from petroleum feeds

Systems and processes are disclosed for producing petrochemical products, such as ethylene, propene and other olefins from crude oil in high severity fluid catalytic cracking (HSFCC) units. Processes include separating a crude oil into a light fraction and a heavy fraction, cracking the light fraction and heavy fraction in separation cracking reaction zones, and regenerating the cracking catalysts in a two-zone regenerator having a first regeneration zone for the first catalyst (heavy fraction) and a second regeneration zone for the second catalyst (light fraction) separate from the first regeneration zone. Flue gas from the first catalyst regeneration zone is passed to the second regeneration zone to provide additional heat to raise the temperature of the second catalyst of the light fraction side. The disclosed systems and processes enable different catalysts and operating conditions to be utilized for the light fraction and the heavy fraction of a crude oil feed.

Process for Obtaining a Catalyst Composite

A process for obtaining a catalyst composite comprising the following steps: 135-. (canceled)36. A process for the catalytic cracking of an olefin-rich feedstock which is selective towards light olefins in the effluent , the process comprising: at least 10 wt % of a molecular sieve having pores of 10-or more-membered rings;', 'at least one metal silicate different from said molecular sieve comprising at least one alkaline earth metal, such that the catalyst composite comprises at least 0.1 wt % of silicate to produce an effluent with an olefin content of lower molecular weight than that of the hydrocarbon feedstock., 'contacting a hydrocarbon feedstock containing one or more olefins with a catalyst composite comprising37. The process according to claim 36 , wherein the molecular sieve is a P-modified zeolite claim 36 , and wherein the metal silicate comprises one or more of Ga claim 36 , Al claim 36 , Ce claim 36 , In claim 36 , Cs claim 36 , Sc claim 36 , Sn claim 36 , Li claim 36 , Zn claim 36 , Co claim 36 , Mo claim 36 , Mn claim 36 , Ni claim 36 , Fe claim 36 , Cu claim 36 , Cr claim 36 , Ti claim 36 , and V.38. The process according to claim 36 , wherein the molecular sieve is a zeolite claim 36 , wherein the metal silicate is xonotlite (CaSiO(OH)).39. The process according to claim 36 , wherein the catalyst composite comprises metal phosphate.40. The process according to claim 36 , wherein the catalyst composite comprises matrix material.41. The process according to claim 36 , wherein the catalyst composite comprises binder.42. The process of comprising: at least 10 wt % of a molecular sieve having pores of 10-or more-membered rings;', 'at least one metal silicate, different from said molecular sieve, comprising at least one alkaline earth metal, such that the XTO catalyst composite comprises at least 0.1 wt % of silicate,, 'contacting an oxygen-containing, halogenide-containing or sulphur-containing organic feedstock in an XTO reactor with an XTO catalyst ...

Oxygenated Hydrocarbon Conversion Zoned Method

Processes are provided for conversion of oxygenated hydrocarbon, such as methanol and/or dimethyl ether, to aromatics, such as a para-xylene, and olefins, such as ethylene and propylene. The processes entail using a reactor having multiple reaction zones where each zone is prepared to promote desired reactions.

AROMATIZATION OF LIGHT HYDROCARBONS USING METAL-DOPED ZEOLITE CATALYSTS WITH ENHANCED MESOPOROSITY

According to embodiments, a process for aromatizing hydrocarbons may include contacting the hydrocarbons with a zinc- or gallium-doped ZSM-5 catalyst having a mesopore volume of greater than 0.09 cm/g. Contacting the hydrocarbons with the catalyst causes a least a portion of the hydrocarbons to undergo chemical reactions to form aromatic hydrocarbons.

DEVICE AND METHOD FOR PREPARING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS FROM METHANOL AND/OR DIMETHYL ETHER AND BENZENE

A fast fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of benzene, the yield of para-xylene, and the selectivity of light olefins are increased. 124-. (canceled)25. A fast fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene , wherein the fast fluidized bed reactor comprises a first reactor feed distributor and a plurality of second reactor feed distributors , the first reactor feed distributor and the plurality of second reactor feed distributors are sequentially arranged along the gas flow direction in the fast fluidized bed reactor.26. The fast fluidized bed reactor of claim 25 , wherein the number of the second reactor feed distributors is in a range from 2 to 10.27. The fast fluidized bed reactor of claim 25 , wherein the fast fluidized bed reactor comprises a first reactor gas-solid separator and a second reactor gas-solid separator claim 25 , the first reactor gas-solid separator is placed in a dilute phase zone or outside a reactor shell claim 25 , and the second reactor gas-solid separator is placed in the dilute phase zone or outside the reactor shell;the first reactor gas-solid separator is provided with a regenerated catalyst inlet, a catalyst outlet of the first reactor gas-solid separator is placed at the bottom of a reaction zone, and a gas outlet of the ...

PRODUCTION OF PROPYLENE IN A FLUID CATALYTIC CRACKING UNIT

A process and apparatus for catalytic cracking of hydrocarbon feedstock employing circulating fluidized bed reactor-regenerator configuration for maximizing the yield of propylene (C3 olefin) is disclosed. The apparatus comprises two reaction zones operating under different temperature and weight hourly space velocity (WHSV), one primary zone for cracking of hydrocarbon feedstock and other as secondary zone for cracking of C4 fraction produced from the cracking of hydrocarbon feedstock in the primary reaction zone, optionally admixed with C4 stream from external source. Two dedicated conduits equipped with valves for control of catalyst flow rate are provided to supply the hot catalyst from a common catalyst regeneration zone wherein the catalyst flowing though conduit connected to the secondary reaction zone is cooled employing a heat exchanging device. The lower temperature achieved in secondary reaction zone on account of exchange of heat along with lower weight hourly space velocity (WHSV) selectively promotes oligomerisation of C4 fraction before being cracked to produce C3 olefin in the subsequent portion of the reaction zone (primary). 1. A process for enhancing the yield of C3 olefin in fluid catalytic cracking of hydrocarbon feedstock , the process comprising:a) contacting a hydrocarbon feedstock in a primary reaction zone of a riser in the presence of a fluidizable solid micro-spherical cracking catalyst to produce cracked hydrocarbon products and spent catalyst;b) separating the spent catalyst from the cracked hydrocarbon products and stripping the spent catalyst with steam to remove the hydrocarbons entrapped inside the pores;c) separating a C4 hydrocarbon fraction of the cracked hydrocarbon products to obtain a recycle C4 hydrocarbon fraction;d) burning off the coke deposited on the spent catalyst in a catalyst regenerator to obtain a hot regenerated catalyst;e) recycling a part of the hot regenerated catalyst into the primary reaction zone and ...

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

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

Treatment of Aromatic Alkylation Feedstock

In a process and system for treatment of feed stocks comprising alkylating agent and metal salts, the metal salts are removed from the feedstock by an efficient combination of separations processes. The processes may take place in one or more stages, each stage taking place in one or more vessels. Such treatment processes may remove 99.9% or more of metal salts from a feedstock, while recovering 99.9% or more of the alkylating agent from the feedstock for use in an alkylation reaction, especially of aromatics such as toluene and benzene. Preferred alkylating agents include methanol and mixtures of carbon monoxide and hydrogen, for methylation of toluene and/or benzene. The methylation proceeds over an aluminosilicate catalyst and preferably yields para-xylene with 75% or greater selectivity. 1. A process for producing para-xylene , the process comprising:(a) separating a feedstock comprising an alkylating agent and a metal salt into at least an alkylating agent-rich vapor stream and a metal salt-enriched liquid blowdown comprising alkylating agent and metal salt; and(b) reacting at least a portion of the alkylating agent-rich vapor stream with one or more aromatic compounds in the presence of an aluminosilicate zeolite catalyst under conditions sufficient to yield para-xylene.2. The process of claim 1 , further comprising:(c) treating the metal salt-enriched liquid blowdown so as to provide at least one additional alkylating agent-rich vapor stream and a metal salt-rich liquid discharge; and(d) reacting at least a portion of the at least one additional alkylating agent-rich vapor stream with one or more aromatic compounds in the presence of the aluminosilicate zeolite catalyst under conditions sufficient to yield para-xylene.3. The process of claim 2 , wherein treating the metal salt-enriched liquid blowdown in step (c) comprises:(c1) sorbing at least a portion of the metal salt from the metal salt-enriched liquid blowdown so as to form at least an alkylating agent- ...

PROCESSES AND COMPOSITIONS FOR TOLUENE METHYLATION IN AN AROMATICS COMPLEX

This present disclosure relates to processes and compositions for toluene methylation in an aromatics complex for producing paraxylene. More specifically, the present disclosure relates to a process for producing paraxylene which includes alkylating a toluene stream and a methanol stream in a toluene methylation zone operating under toluene methylation conditions in the presence of a catalyst comprising a MFI crystal to produce a toluene methylation product stream. 1. A process for producing paraxylene comprising alkylating a toluene stream and a methanol stream in a toluene methylation zone operating under toluene methylation conditions in the presence of a catalyst comprising an MFI crystal , alone or bound to any another material , to produce a toluene methylation product stream.2. The process according to claim 1 , wherein the catalyst includes MFI crystals with a framework silica to alumina ratio of about 50 to about 10 claim 1 ,000 claim 1 , more preferably about 100 to about 6 claim 1 ,000 claim 1 , or even more preferably about 500 to about 3 claim 1 ,000.3. The process according to claim 1 , wherein the toluene methylation conditions include a temperature of about 250° C. to about 750° C. claim 1 , more preferably between about 350° C. and about 650° C. claim 1 , even more preferably between about 400° C. and about 600° C.4. The process according to claim 1 , wherein the toluene methylation conditions include a pressure of about 1 Barg to about 100 Barg claim 1 , more preferably between about 1 Barg to about 50 Barg claim 1 , even more preferably between 2 Barg to about 30 Barg.5. The process according to claim 1 , wherein the toluene methylation product stream has a benzene to total xylene molar ratio of less than 1 claim 1 , or preferably less than 0.5 claim 1 , or more preferably less than 0.16. The process according to claim 2 , wherein the catalyst includes MFI crystals with a framework silica to alumina ratio of 2000.7. The process according to claim ...

SYSTEMS AND METHODS FOR PRODUCING PROPYLENE

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

FLUIDIZED BED UNIT STARTUP

The startup of a fluidized bed process unit uses an air heater to raise the temperature of the unit to the level necessary for operation of the unit to be self-sustaining in its normal operating regime without the use of torch oil. This startup sequence is particularly useful for fluidized bed units which utilize a circulating catalyst with particular emphasis on endothermic conversion units such as FCC and Resid Catalytic Cracking (RCC), but also on other catalytic units with circulating catalyst inventories such as various exothermic conversion, e.g. methanol conversion, processes. Elimination of the torch oil injection enables catalyst selectivity/activity to be retained during startup and at any other time that the heat requirement of the unit cannot be met by the internal functioning of the process, e.g. by coke generation during the reaction and combustion during regeneration of the catalysts or during the reaction itself. 1. A fluidized bed hydrocarbon conversion process in which a feed stream is converted in a fluidized bed process unit at an elevated temperature , comprising the step of starting up the unit by heating the unit to a self-sustaining reaction temperature with heated air from a heater.2. A process according to in which the unit is heated to a self-sustaining reaction temperature exclusively with heated air from an air heater.3. A process according to in which the unit is heated to a self-sustaining reaction temperature without burning hydrocarbon oil in the unit.4. A process according to in which the conversion process is an endothermic conversion process.5. A process according to in which the endothermic conversion process comprises Fluid Catalytic Cracking (FCC) of a heavy hydrocarbon feed.6. A process according to in which the conversion process is an exothermic conversion process.7. A process according to in which the conversion process comprises methanol conversion to aromatics or olefins.8. A fluidized bed catalytic cracking process in ...

Process for oligomerizing gasoline without further upgrading

Oligomerizing C 4 and C 5 olefins over a SPA catalyst provides an oligomerate product stream comprising C 6 + olefins that meets a gasoline T-90 specification of 380° F. The oligomerate product stream can be taken to the gasoline pool without further upgrading.

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Integrated systems are provided for the production of higher hydrocarbon compositions, for example liquid hydrocarbon compositions, from methane using an oxidative coupling of methane system to convert methane to ethylene, followed by conversion of ethylene to selectable higher hydrocarbon products. Integrated systems and processes are provided that process methane through to these higher hydrocarbon products. 1. A system , comprising:{'sub': 2', '4', '2', '4', '3', '6', '2', '2', '4, 'an ethylene-to-liquids (ETL) reactor that (i) receives an olefin feed stream at a first temperature, said olefin feed stream comprising (1) ethylene (CH) at a concentration of at least about 0.5 mole percent (mol %), (2) CHand propylene (CH) at a combined concentration of at most about 10 mol %, and (3) carbon monoxide (CO) or carbon dioxide (CO), and (ii) as part of an ETL process, facilitates conversion of CHto higher hydrocarbon products with the aid of an ETL catalyst to yield a product stream comprising said higher hydrocarbon products that is at a second temperature which is higher than said first temperature, wherein said ETL process liberates heat, wherein said higher hydrocarbon products comprise an olefin compound and an aromatic compound; and'}a separations module in fluid communication with said ETL reactor that recovers from said product stream a liquid stream comprising said higher hydrocarbon products, wherein said higher hydrocarbon products include (i) at least 5 compounds having 5 different carbon numbers, said 5 different carbon numbers selected from 4 through 20, wherein each of said at least 5 compounds is at a concentration of at least 5 weight percent (wt %) of said liquid stream, and (ii) a paraffin compound, an isoparaffin compound, and a naphthene compound,wherein at least about 80% of said heat liberated in said ETL process provides a difference between said first temperature and said second temperature of between about 50° C. and about 150° C.2. The system ...

In-situ Trim Coke Selectivation of Toluene Disproportionation Catalyst

The invention relates to treating a molecular sieve prepared by at least one in situ selectivation sequence wherein graphitic coke is adhered to said molecular sieve, which is useful in a toluene disproportionation process. 1. A method for modifying a molecular sieve comprising:treating a molecular sieve prepared by at least one ex situ silicon selectivation sequence to at least one in situ trim coke selectivation sequence to provide a modified silicon selectivated molecular sieve, wherein graphitic coke is adhered to said molecular sieve by said in situ trim coke selectivation sequence.2. The method of claim 1 , wherein said ex situ silicon selectivation sequence comprises:contacting said molecular sieve with a silicon-containing selectivating agent comprising silicones or silicone polymers, to provide a silicon-treated molecular sieve;calcining said silicon-treated molecular sieve to provide a calcined silicon selectivated molecular sieve;optionally steam treating said calcined silicon selectivated molecular sieve.3. The method of claim 1 , wherein said molecular sieve has been modified by between two and six ex situ silicon selectivation sequences and including at least one steam-treating.4. The method of claim 1 , wherein said molecular sieve has been modified by two ex situ silicon selectivation sequences.5. The method of any one of the preceding claims claim 1 , wherein said molecular sieve has been modified by three ex situ silicon selectivation sequences.6. The method of claim 1 , wherein the in situ trim coke selectivation conditions comprise a reactor temperature of about 260-593° C. claim 1 , for about 0.1 hour to about 3 weeks claim 1 , operating at a WHSV of about 0.1-20 hr claim 1 , and a hydrogen partial pressure of about 0.0689-2.07 Mpa-a claim 1 , with a reactor pressure of about 1.72-2.41 Mpa-g.7. The method of claim 6 , wherein the in situ trim coke selectivation conditions comprise a reactor temperature of about 454-510° C. claim 6 , operating at ...

ETHANOL DEHYDRATION CATALYST FOR ENERGY SAVING AND METHOD OF MANUFACTURING ETHYLENE USING SAME

Provided are an ethanol dehydration catalyst having a high ethylene yield even at a low temperature region, as an ethanol dehydration catalyst for converting a feedstock including anhydrous ethanol or hydrous ethanol to ethylene, and a method of preparing ethylene by using the same. In the ethanol dehydration catalyst for converting a feedstock including anhydrous ethanol or hydrous ethanol to ethylene of the present invention, the catalyst includes 0.1 wt % to 0.5 wt % of lanthanum (La) or 0.05 wt % to 1 wt % of gallium (Ga) in ZSM-5. 1. An ethanol dehydration catalyst for converting a feedstock comprising anhydrous ethanol or hydrous ethanol to ethylene ,wherein the catalyst comprises 0.1 wt % to 0.5 wt % of lanthanum (La) in ZSM-5.2. The ethanol dehydration catalyst of claim 1 , further comprising 0.01 wt % to 1 wt % of phosphorous (P).3. An ethanol dehydration catalyst for converting a feedstock comprising anhydrous ethanol or hydrous ethanol to ethylene claim 1 ,wherein the catalyst comprises 0.05 wt % to 1 wt % of gallium (Ga) in ZSM-5.4. The ethanol dehydration catalyst of claim 3 , further comprising 0.05 wt % to 0.5 wt % of La.5. The ethanol dehydration catalyst of claim 1 , wherein the hydrous ethanol has a water content of 30 wt % or less.6. The ethanol dehydration catalyst of of claim 1 , wherein the ZSM-5 has a Si/Al2 molar ratio of 20 to 45.7. The ethanol dehydration catalyst of claim 1 , wherein the catalyst has an ethanol conversion rate of 98% or more and an ethylene selectivity of 98% or more which are measured under a condition:[measurement condition]the ethanol conversion rate and the ethylene selectivity are measured after dehydration at a space velocity (WHSV) of 5 hr-1 and a temperature of 240° C. for 240 hours.8. The ethanol dehydration catalyst of claim 3 , wherein the catalyst has an ethanol conversion rate of 99% or more and an ethylene selectivity of 96% or more which are measured under a condition:[measurement condition]the ethanol ...

Zsm-5 catalyst

Disclosed in certain embodiments are ZSM-5 zeolite microspheres. Disclosed in certain embodiments is a method of forming ZSM-5 zeolite microspheres including: 1) shaping a mixture into microspheres where the mixture includes a silica material and of particulates selected from at least one high-density material with an absolute bulk density of at least 0.3 g/cc, ZSM-5 zeolite crystals, and combinations thereof; 2) calcining the microspheres; and 3) reacting and subsequently heating the microspheres with at least one alkali solution to form ZSM-5 zeolite in-situ on the microspheres, where the ZSM-5 zeolite microspheres contain substantially no clay or calcined clay material.

Transalkylation System

The invention relates to a transalkylation system to convert feedstreams containing benzene and/or toluene (C7− aromatic hydrocarbons) and feedstreams containing C9+ aromatic hydrocarbons into a product stream comprising xylenes.

Method for preparing aromatic hydrocarbon with carbon dioxide hydrogenation

A method for preparing aromatic hydrocarbons with carbon dioxide hydrogenation, comprising: directly converting a mixed gas consisting of carbon dioxide and hydrogen with the catalysis of a composite catalyst under reaction conditions of a temperature of 250-450° C., a pressure of 0.01-10.0 MPa, a feedstock gas hourly space velocity of 500-50000 mL/(h·g cat ) and a H 2 /CO 2 molar ratio of 0.5-8.0, to produce aromatic hydrocarbons. The composite catalyst is a mixture of a first component and a second component. The first component is an iron-based catalyst for making low-carbon olefin via carbon dioxide hydrogenation, and the second component is at least one of metal modified or non-modified molecular sieves which are mainly used for olefin aromatization. In the method, CO 2 conversion per pass may be above 33%, the hydrocarbon product selectivity may be controlled to be above 80%, the methane content is lower than 8%, C 5+ hydrocarbon content is higher than 65% and the proportion of the aromatic hydrocarbons in C 5+ hydrocarbons may be above 63%.

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Integrated systems are provided for the production of higher hydrocarbon compositions, for example liquid hydrocarbon compositions, from methane using an oxidative coupling of methane system to convert methane to ethylene, followed by conversion of ethylene to selectable higher hydrocarbon products. Integrated systems and processes are provided that process methane through to these higher hydrocarbon products. 1111.-. (canceled)112. A method , comprising:(a) directing an olefin-containing stream comprising an olefin into an ethylene-to-liquids (ETL) reactor comprising an ETL catalyst that facilitates conversion of at least a portion of said olefin to higher hydrocarbon compounds to yield an ETL product stream comprising said higher hydrocarbon compounds;{'sub': 4+', '3, '(b) directing at least a portion of said ETL product stream into a de-propanizer that separates said higher hydrocarbon compounds into a bottom stream comprising hydrocarbon compounds with four or more carbon atoms (C compounds) and an overhead stream comprising hydrocarbon compounds with three carbon atoms (Ccompounds); and'}{'sub': '3', '(c) directing at least a portion of said Ccompounds into said ETL reactor.'}113. The method of wherein said olefin comprises ethylene claim 112 , propylene claim 112 , or a combination thereof.114. The method of claim 112 , further comprising claim 112 , prior to (a) claim 112 , directing a hydrocarbon feedstream comprising feedstream hydrocarbons into a cracking reactor comprising a cracking catalyst that facilitates a cracking of said feedstream hydrocarbons to produce a cracked stream comprising cracked hydrocarbons claim 112 , wherein said cracked hydrocarbons have a lower molecular weight than said feedstream hydrocarbons claim 112 , and using at least a subset of said cracked hydrocarbons to generate said olefin-containing stream.115. The method of claim 114 , further comprising directing said cracked stream into a separations unit that separates said ...

Processes for conversion of biologically derived mevalonic acid

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

Catalyst Comprising a Phosphorous Modified Zeolite and Having Partly an Alpo Structure

The present invention relates to a catalyst comprising a phosphorus modified zeolite, said phosphorus modified zeolite having partly an ALPO structure, wherein, the catalyst comprises a P-modified zeolite and a binder, the zeolite comprises at least one ten members ring in the structure, optionally the catalyst comprises one or more metal oxides, the ALPO structure is determined by a signal between 35-45 ppm in Al MAS NMR spectrum. 132-. (canceled)33. A method to make a phosphorus modified zeolite comprising:a) providing a zeolite comprising at least one ten member ring in the structure thereof, and optionally steaming the zeolite;b) mixing the zeolite of step a) with at least a component selected among one or more binders and shaping additives, and then shaping the mixture;c) optionally making a ion-exchange;d) optionally steaming the shaped mixture, optionally before step c);e) introducing phosphorus on the catalyst to introduce at least 0.1 wt % of the phosphorus;f) optionally introducing a metal, optionally simultaneously with step e);g) optionally washing the catalyst;h) optionally calcinating the catalyst; andi) steaming the catalyst;{'sup': '27', 'wherein the phosphorus modified zeolite has partly an ALPO structure, and wherein the ALPO structure is determined by a signal between 35-45 ppm in Al MAS NMR spectrum.'}34. The method of claim 33 , wherein claim 33 , at least one of the steaming of step d) and the steaming of step a) is mandatory; andwherein introduction of the phosphorus is made by dry impregnation or chemical vapor deposition.35. The method of claim 33 , wherein claim 33 , at least one of the steaming of step d) and the steaming of step a) is mandatory; andwherein step i) is performed by steaming at a steaming severity (X) of at least about 2.36. The method of claim 33 , wherein the metal is introduced.37. The method of claim 36 , wherein the metal is calcium.38. The method of claim 33 , wherein the zeolite is MFI claim 33 , MTT claim 33 , FER ...

PROCESS FOR SELECTIVE PRODUCTION OF LIGHT OLEFINS AND AROMATIC FROM CRACKED LIGHT NAPHTHA

The present invention provides a process for a production of light olefins and aromatics from cracked light naphtha by selective cracking. The present invention thus provides a process for up grading cracked olefinic naphtha to high value petrochemical feed stocks. This process is based on catalytic cracking in which the catalyst activity is optimized by depositing coke for production of light olefins and aromatics. The proposed process has high flexibility and can be operated either in maximizing olefins as reflected from the PIE ratio or in maximizing aromatics (BTX) at different modes of operation depending upon the product requirement. 1. A process for selective production of light olefins and aromatics , the process comprising:a) feeding a mixed olefinic cracked naphtha feedstock into a reactor; (i) wherein under olefinic mode of operation, the mixed olefinic cracked naphtha is catalytically cracked by contacting with a zeolite catalyst for a residence time ranging between 35-65 minutes and at a pressure ranging between 1-2 bar to obtain a cracked product comprising light olefins in the range of 30-50 wt % and obtaining the light olefins as a gaseous product with a propylene to ethylene ratio (PIE) in the range of 1-5;', '(ii) wherein under aromatic mode of operation, the mixed olefinic cracked naphtha is catalytically cracked by contacting with a zeolite catalyst for a residence time ranging between 20-35 minutes and at a pressure ranging between 5-7 bar to obtain a cracked product comprising aromatics in the range of 10-25 wt % and obtaining the aromatics as a liquid product; and, 'b) catalytic cracking of the mixed olefinic cracked naphtha in the reactor under olefinic mode or aromatic mode of operation,'}c) recovering spent catalyst from the reactor and feeding the spent catalyst to a regenerator to obtain a regenerated catalyst and recycling the regenerated catalyst to the reactor.2. The process as claimed in claim 1 , wherein the mixed olefinic cracked ...

Production of Aromatics from Methanol and Co-Feeds

Methods are provided for improving the yield of aromatics during conversion of oxygenate feeds. An oxygenate feed can contain a mixture of oxygenate compounds, including one or more compounds with a hydrogen index of less than 2, so that an effective hydrogen index of the mixture of oxygenates is between about 1.4 and 1.9. Methods are also provided for converting a mixture of oxygenates with an effective hydrogen index greater than about 1 with a pyrolysis oil co-feed. The difficulties in co-processing a pyrolysis oil can be reduced or minimized by staging the introduction of pyrolysis oil into a reaction system. This can allow varying mixtures of pyrolysis oil and methanol, or another oxygenate feed, to be introduced into a reaction system at various feed entry points.

Conversion of Acetylene and Methanol to Aromatics

Methods are provided for forming aromatic compounds from a highly unsaturated aliphatic feeds optionally in combination with methanol. The method can include dehydrogenating a feed containing at least about 50 vol % C-Calkanes under dehydrogenation conditions to form a dehydrogenation effluent containing at least about 25 vol % alkynes. Alternatively, other sources of alkyne-containing feeds can be used. At least a portion of the alkyne-containing feed can then be converted under effective conversion conditions to form a conversion effluent comprising a hydrocarbon product containing aromatic compounds. 1. A method for forming aromatic compounds , comprising:{'sub': 1', '4, 'dehydrogenating a feed containing at least about 50 vol % C-Calkanes under dehydrogenation conditions to form a dehydrogenation effluent containing at least about 25 vol % alkynes, the dehydrogenation conditions including a temperature of at least about 1000° C.; and'}converting at least a portion of the dehydrogenation effluent under effective conversion conditions with an aromatization catalyst to form a conversion effluent comprising a hydrocarbon product containing aromatic compounds, a volume percentage of aromatic compounds in the hydrocarbon product being at least about 10 vol % greater than a volume percentage of aromatic compounds in the dehydrogenation effluent.2. The method of claim 1 , wherein the feed containing at least about 50 vol % C-Calkanes comprises at least about 75% Calkanes.3. The method of claim 1 , wherein the feed containing at least about 50 vol % C-Calkanes is dehydrogenated in a reverse flow reaction system.4. The method of claim 1 , wherein converting at least a portion of the dehydrogenation effluent under effective conversion conditions comprises converting the at least a portion of the dehydrogenation effluent in the presence of methanol.5. The method of claim 1 , wherein the effective conversion conditions comprise exposing the dehydrogenation effluent to a ...

Catalyst and Its Use in Dehydrocyclization Processes

The invention relates to catalysts and their use in processes for dehydrocyclization of light paraffinic hydrocarbon feedstock to higher-value hydrocarbon, such as aromatic hydrocarbon, to dehydrocyclization catalysts useful in such processes, and to the methods of making such catalysts. One of more of the dehydrocyclization catalysts comprising a crystalline aluminosilicate zeolite having a constraint index of less than or equal to about 12, at least one Group 3 to Group 13 metal of the IUPAC Periodic Table and phosphorous.

Catalyst and Its Use in Hydrocarbon Conversion Process

The invention relates to catalysts and their use in processes for conversion of hydrocarbon feedstock to a product comprising single-ring aromatic hydrocarbons having six or more carbon atoms, to the methods of making such catalysts, to processes for using such catalysts, and to apparatus and systems for carrying out such processes. One of more of the catalysts comprise a crystalline aluminosilicate having a Constraint Index in the range of 1 to 12, a first metal and/or a second metal, and at least one selectivating agent, such as, for example, an organo-silicate. 1. A catalyst comprising:(a) a crystalline aluminosilicate having a Constraint Index in the range of 1 to 12;(b) a first metal; and(c) at least one selectivating agent selected from the group consisting of an organo-aluminate, an organo-phosphate, and mixtures thereof.2. The catalyst of claim 1 , further comprising a second metal claim 1 , wherein said second metal is different from said first metal.3. A catalyst comprising:(a) a crystalline aluminosilicate having a Constraint Index in the range of 1 to 12;(b) a first metal and a second metal, wherein said second metal is different from said first metal; and(c) at least one organo-silicate selectivating agent.4. The catalyst of claim 3 , wherein said second metal is selected from the group consisting of lanthanum claim 3 , rhenium claim 3 , silver claim 3 , palladium claim 3 , tin claim 3 , molybdenum claim 3 , and mixtures of two or more thereof.5. The catalyst of claim 3 , wherein said second metal is lanthanum.6. The catalyst of claim 3 , wherein said catalyst has from about 0.005 wt. % to about 1.5 wt. % of said second metal claim 3 , based on the weight of said catalyst.7. The catalyst of claim 3 , wherein said organo-silicate selectivating agent is a tetraalkyl orthosilicate selected from the group consisting of a tetramethyl orthosilicate (TMOS) claim 3 , a tetraethyl orthosilicate (TEOS) claim 3 , a tetrapropyl orthosilicate (TPOS) claim 3 , and ...

Mel-Type Zeolite for Converting Aromatic Hydrocarbons, Process for Making and Catalytic Composition Comprising Said Zeolite

Novel MEL framework type zeolites can be made to have small crystallite sizes and desirable silica/SiCb molar ratios. Catalyst compositions comprising such MEL framework type zeolites can be particularly advantageous in isomerization C8 aromatic mixtures. An isomerization process for converting C8 aromatic hydrocarbons can advantageously utilize a catalyst composition comprising a MEL framework type zeolite.

Xylene Isomerization Process and Catalyst Therefor

The invention concerns a xylenes isomerization process for the production of equilibrium or near-equilibrium xylenes. The process utilizes a catalyst comprising HZSM-5 or MCM-49 and process conditions including a temperature of less than 295° C. and a pressure sufficient to maintain the xylenes in liquid phase. In embodiments, the process can be operated in a continuous mode with ppm levels of dissolved H 2 in the feed and in other embodiments in a cyclic mode without the H 2 in feed but with periodic regenerations using a feed having low ppm levels of H 2 .

PROCESS TO PREPARE PROPYLENE

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

Process to Make Olefins from Oxygenates

The present invention relates to a process to make light olefins, in a combined XTO-OC process, from an oxygen-containing, halogenide-containing or sulphur-containing organic feedstock comprising: 119-. (canceled)20. A process of making light olefins comprising:selecting a molecular sieve having pores of 10-or more-membered rings;contacting the molecular sieve with a metal silicate comprising at least one alkaline earth metal to form a catalyst composite comprising at least 0.1 wt % of silicate;providing an oxygen-containing, halogenide-containing, or sulphur-containing organic feedstock;providing an oxygenate to olefin (XTO) reaction zone, an olefin cracking (OC) reaction zone, and a catalyst regeneration zone, wherein one or more catalysts are in the XTO reaction zone and the same one or more catalysts are in the OC reaction zone, wherein each of the one or more catalysts is a molecular sieves containing at least 10 membered rings pore opening in their microporous structure, and wherein the at least one of the catalysts is the catalyst composite;wherein the one or more catalysts circulate in the three zones, such that at least a portion of regenerated one or more catalysts is passed to the OC reaction zone, at least a portion of the one or more catalysts in the OC reaction zone is passed to the XTO reaction zone and at least a portion of the one or more catalysts in the XTO reaction zone is passed to the catalyst regeneration zone;contacting the oxygen-containing, halogenide-containing or sulphur-containing organic feedstock in the XTO reaction zone with the one or more catalysts at conditions effective to convert at least a portion of the feedstock to form an XTO reaction zone effluent comprising light olefins and a heavy hydrocarbon fraction;separating the light olefins from the heavy hydrocarbon fraction; andcontacting the heavy hydrocarbon fraction in the OC reaction zone with the one or more catalysts at conditions effective to convert at least a portion of ...

PROCESS FOR PRODUCING SHORT-CHAIN OLEFINS WITH PROLONGED CYCLE TIME

A process for producing short-chain olefins by conversion of oxygenates in a multi-stage fixed-bed reactor, in which the individual stages for reaction zones are covered with beds of a granular, form-selective zeolite catalyst and the feed mixture containing oxygenates is added distributed over the reaction stages. An increase of the availability of the fixed-bed reactor for the olefin production with the same or an increased yield of short-chain olefins is achieved in that one or more reaction zones are charged with a distinctly reduced mass flow of the feed mixture containing oxygenates, wherein the reduced mass flow fraction is distributed over other reaction zones. 1. A process for producing a hydrocarbon product comprising ethylene and propylene , by converting a starting material mixture comprising steam and an oxygenate to one or more olefins under oxygenate conversion conditions in a reactor , the starting material mixture being divided into several partial streams , the process comprising:charging a first reaction zone of the reactor with steam and a first partial stream comprising the starting material mixture, the reactor comprising a plurality of series-connected reaction zones in fluid connection with each other, the reactor comprising a first reaction zone and at least one succeeding reaction zone;charging the at least one succeeding reaction zone with a second partial stream comprising the starting material mixture; andadditionally charging each of the at least one succeeding reaction zones with a product stream from an upstream reaction zone; andfurther charging at least one of the at least one succeeding reaction zone with a reduced partial stream comprising the starting material mixture,wherein the reduced partial stream is smaller than a partial stream supplied to the upstream reaction zone.2. The process of claim 1 , wherein the reduced partial stream is not more than 70% of a next larger partial stream.3. The process of claim 1 , herein the ...

Modified Y-Zeolite/ZSM-5 Catalyst For Increased Propylene Production

Provided is a Fluid Catalytic Cracking catalyst composition having increased propylene production with respect to other Fluid Catalytic Cracking catalysts (measured at constant conversion). The catalyst composition comprises a particulate which comprises (a) non-rare earth metal exchanged Y-zeolite in an amount in the range of about 5 to about 50 wt %, based upon the weight of the particulate; and (b) ZSM-5 zeolite in an amount in the range of about 2 to about 50 wt %, based upon the weight of the particulate.

SEPARATION DEVICE FOR USE IN FLUIDIZED BED REACTOR, REACTION REGENERATION APPARATUS AND PROCESS FOR PREPARING OLEFINS, AND PROCESS FOR PREPARING AROMATIC HYDROCARBONS

Device for use in a fluidized bed reactor includes a gas-solid separator communicated with an outlet of the fluidized bed reactor; a vertically arranged damper, a solid outlet of the gas-solid separator communicated with a lower region of the damper, a gas outlet of the gas-solid separator communicated with an upper region of the damper; a fine gas-solid separator, an inlet of the fine gas-solid separator communicated with the upper region of the damper, and a solid outlet of the fine gas-solid separator communicated with the lower region of the damper. Product from the fluidized bed reactor is fed into the preliminary gas-solid separator, most solid catalysts separated and fed into the lower region; the product entraining the rest catalysts is fed into the upper region, and into the fine gas-solid separator, the rest catalysts fed into the lower region; and final product is obtained from the fine gas-solid separator. 1. A separation device for use in a fluidized bed reactor , comprisinga preliminary gas-solid separator communicated with an outlet of the fluidized bed reactor,a vertically arranged damper, a solid outlet of the preliminary gas-solid separator being communicated with a lower region of the damper, and a gas outlet of the preliminary gas-solid separator being communicated with an upper region of the damper, anda fine gas-solid separator, an inlet of the fine gas-solid separator being communicated with the upper region of the damper, and a solid outlet of the fine gas-solid separator being communicated with the lower region of the damper, whereinthe separation device is configured so that product having catalysts entrained therein from the fluidized bed reactor is fed into the preliminary gas-solid separator, most solid catalysts being separated and fed into the lower region of the damper; the product entraining the rest catalysts is fed into the upper region of the damper, and into the fine gas-solid separator, the rest catalysts being separated and fed ...

APPARATUS AND PROCESS FOR PRODUCING GASOLINE, OLEFINS AND AROMATICS FROM OXYGENATES

Apparatuses and processes for converting an oxygenate feedstock, such as methanol and dimethyl ether, in a fluidized bed containing a catalyst to hydrocarbons, such as gasoline boiling components, olefins and aromatics are provided herein. 1. A process for converting an oxygenate feedstock to a C gasoline product comprising: i. a catalyst; and', 'ii. at least one packing layer;, 'a. feeding the oxygenate feedstock to a fluidized bed reactor under conditions to convert the oxygenate feedstock to a hydrocarbon mixture in a reactor effluent, wherein the fluid bed reactor comprisesb. cooling the reactor effluent comprising the hydrocarbon mixture and condensing a portion of the reactor effluent to form a mixed phase effluent;c. separating the mixed phase effluent into an aqueous liquid phase, a hydrocarbon gas phase and a hydrocarbon liquid phase; and{'sub': 4−', '2', '4', '5+, 'd. separating a C light gas comprising C-Colefins and the C gasoline product from the hydrocarbon gas phase and the hydrocarbon liquid phase.'}2. The process of claim 1 , wherein the temperature in the fluidized bed reactor is about 600° F. to about 900° F.3. The process of claim 1 , wherein the pressure in the fluidized bed reactor is about 25 psig to about 400 psig.4. The process of claim 1 , wherein the catalyst comprises a zeolite.5. The process of claim 1 , wherein the zeolite is ZSM-5.6. The process of claim 1 , wherein the oxygenate feedstock is selected from the group consisting of methanol claim 1 , dimethylether and a combination thereof.7. The process of claim 1 , wherein the fluidized bed reactor comprises at least two packing layers.8. The process of claim 1 , wherein the yield of C gasoline product is at least 80 wt % of HC.9. The process of claim 1 , wherein the yield of C gasoline product is about 80 wt % to about 90 wt % of HC.10. The process of claim 1 , further comprising removing catalyst fines from the reactor effluent.11. The process of claim 1 , further comprising removing ...

FLUIDIZED BED REACTOR, REACTION REGENERATION APPARATUS, PROCESS FOR PREPARING OLEFINS, AND PROCESS FOR PREPARING AROMATIC HYDROCARBONS

A fluidized bed reactor is provided, comprising an inlet zone at a lower position, an outlet zone at an upper position, and a reaction zone between the inlet zone and the outlet zone. A guide plate with through holes is disposed in the reaction zone, comprising a dense channel region in an intermediate region thereof and a sparse channel region disposed on a periphery thereof and encompassing the dense channel region. Catalysts in said fluidized bed reactor can be homogeneously distributed in the reaction zone thereof, whereby the reaction efficiency can be improved. A reaction regeneration apparatus comprising said fluidized bed reactor, and a process for preparing olefins from oxygenates and a process for preparing aromatic hydrocarbons from oxygenates using the reaction regeneration apparatus. 1. A fluidized bed reactor , comprising an inlet zone at a lower position , an outlet zone at an upper position , and a reaction zone between the inlet zone and the outlet zone , whereina guide plate is disposed in the reaction zone, comprising a dense channel region in an intermediate region thereof and a sparse channel region disposed on a periphery thereof encompassing the dense channel region.2. The fluidized bed reactor according to claim 1 , wherein a dimension of a channel in the dense channel region is smaller than that of a channel in the sparse channel region.3. The fluidized bed reactor according to claim 2 , wherein a ratio of the dimension of the channel in the dense channel region to that of the channel in the sparse channel region is in a range of 1:4 to 2:3.4. The fluidized bed reactor according to claim 3 , wherein the dimension of the channel in the dense channel region is in a range of 0.01 m to 0.08 m.5. The fluidized bed reactor according to claim 1 , wherein the dense channel region and the sparse channel region each comprise a circular plate having evenly distributed pores claim 1 , or a plurality of concentric ring shaped sloping panels spaced apart ...

PROCESS FOR THE PREPARATION OF A CATALYST SUPPORT

Process for preparing a catalyst support which process comprises a) mixing pentasil zeolite having a bulk silica to alumina molar ratio in the range of from 20 to 150 with water, a silica source and an alkali metal salt, b) extruding the mixture obtained in step (a), c) drying and calcining the extrudates obtained in step (b), d) subjecting the calcined extrudates obtained in step (c) to ion exchange to reduce the alkali metal content, and e) drying the extrudates obtained in step (d); process for preparing a catalyst by furthermore impregnating such support with platinum in an amount in the range of from 0.001 to 0.1 wt % and tin in an amount in the range of from 0.01 to 0.5 wt %, each on the basis of total catalyst; ethylbenzene dealkylation catalyst obtainable thereby and a process for dealkylation of ethylbenzene which process comprises contacting feedstock containing ethylbenzene with such catalyst. 1. An ethylbenzene dealkylation catalyst , containing; a) mixing pentasil zeolite having a bulk silica to alumina molar ratio in the range of from 20 to 150 with water, a silica source and an alkali metal salt;', 'b) extruding the mixture obtained in step (a);', 'c) drying and calcining the extrudates obtained in step (b);', 'd) treating the extrudates obtained in step (c) with an aqueous solution of fluorosilicate salt to provide fluorosilicate-treated extrudates;', 'e) subjecting the fluorosilicate-treated extrudates obtained in step (d) to ion exchange with an aqueous ammonium containing solution to reduce the alkali metal content; and', 'f) drying the extrudates obtained in step (e); and, 'a support obtainable by a process which comprisesplatinum in an amount in the range of from 0.001 to 0.1 wt % and tin in an amount in the range of from 0.01 to 0.5 wt %, each on the basis of total catalyst.2. An ethylbenzene dealkylation catalyst as recited in claim 1 , wherein the silica source is selected from the group consisting of powder form silica claim 1 , silica sol ...

Processes for Producing Aromatic Hydrocarbon, p-Xylene and Terephthalic Acid

The present invention relates to a process for preparing an aromatic hydrocarbon, and processes for producing p-xylene and terephthalic acid. The process for producing said aromatic hydrocarbon comprises a step of contacting an olefin with a diene in the presence of a catalyst to produce an aromatic hydrocarbon, which is characterized in that, at least a part of said olefin is substituted with dienophile. The reaction pressure can be reduced and the xylene selectivity can be increased with the improvement of the present invention. 2. The process according to claim 1 , wherein said catalyst is a molecular sieve claim 1 , and said molecular sieve is one or more selected from ZSM-type molecular sieve (preferably one or more selected from ZSM-5 claim 1 , ZSM-11 claim 1 , ZSM-22 claim 1 , ZSM-23 and ZSM-38) claim 1 , Y-type molecular sieve claim 1 , beta-type molecular sieve and MCM-type molecular sieve (preferably one or more selected from MCM-22 and MCM-41); preferably one or more selected from ZSM-5 claim 1 , Y-type molecular sieve claim 1 , beta-type molecular sieve and MCM-41; more preferably ZSM-5.3. The process according to claim 2 , wherein said ZSM-type molecular sieve (preferably ZSM-5 or ZSM-22) has a SiO2/Al2O3 molar ratio of 10-500 claim 2 , preferably 15-200; said Y-type molecular sieve has a SiO2/Al2O3 molar ratio of 2-80 claim 2 , preferably 3-50; said beta-type molecular sieve has a SiO2/Al2O3 molar ratio of 10-150 claim 2 , preferably 15-65; said MCM-type molecular sieve (preferably MCM-22 or MCM-41) has a SiO2/Al2O3 molar ratio of 20-250 claim 2 , preferably 40-150.4. The process according to claim 1 , wherein the ratio of the mole of said diene to the total mole of said dienophile and said olefin is 0.1-10 claim 1 , preferably 0.5-2.5. The process according to claim 1 , wherein said contacting step is conducted at a reaction temperature of 80 to 400° C. claim 1 , preferably 160 to 350° C. claim 1 , under a reaction pressure of 0.5 to 10 MPa claim 1 , ...

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

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

OXYGENATE-TO-OLEFINS PROCESS AND AN APPARATUS THEREFOR

The present invention relates to a process for the preparation of an olefinic product, such as one or both of ethylene and propylene, from an oxygenate feedstock, such as methanol, and an apparatus therefore, said process comprising: treating an effluent stream with a carbonyl compound absorbent stream comprising an aqueous solution of bisulphite having a pH in the range of from 4 to 8, to provide an olefinic product stream comprising olefin and a loaded carbonyl compound absorbent stream comprising an aqueous solution of at least one carbonyl adduct comprising one or both of C2+ aldehyde adduct and ketone adduct and optionally unreacted bisulphite, said liquid absorbent stream and loaded carbonyl compound absorbent stream in a carbonyl compound absorbent circuit separate from the effluent separation circuit. 1. A process for the preparation of olefinic product , the process comprising at least the steps of:reacting an oxygenate feedstock comprising oxygenate in an oxygenate reaction zone in the presence of a catalyst comprising a molecular sieve to produce a reaction effluent stream comprising oxygenate, olefin, water and carbonyl compound comprising formaldehyde and one or both of C2+ aldehyde and ketone;treating the reaction effluent stream with an aqueous liquid stream to provide a water rich stream comprising oxygenate, formaldehyde and water and a water depleted effluent stream comprising olefin and carbonyl compound comprising one or both of C2+ aldehyde and ketone, said aqueous liquid stream and said water rich stream present in an effluent separation circuit;compressing the water depleted effluent stream, with the optional removal of any condensed phase, to provide a compressed effluent stream; andtreating the compressed effluent stream with a carbonyl compound absorbent stream comprising an aqueous solution of bisulphite having a pH in the range of from 4 to 8, to provide an olefinic product stream comprising olefin and a loaded carbonyl compound absorbent ...

Increased oligomer selectivity from olefin oligomerization by incorporation of boron

A novel catalyst composition and its use in the oligomerization reactions of light alkenes to higher molecular weight hydrocarbons. The catalyst comprises boron added to an Al-containing or Ga-containing or Fe-containing support. The catalyst composition is an active and selective catalyst for the catalytic oligomerization reactions of light alkenes to higher molecular weight hydrocarbons.

DUAL STAGE LIGHT ALKANE CONVERSION TO FUELS

A process and system for the conversion of a feedstock comprising C3-C5 light alkanes to a C5+ hydrocarbon product, for example, a BTX-rich hydrocarbon product, by performing the alkane activation (first-stage) and the oligomerization/aromatization (second-stage) in separate stages, which allows each conversion process to occur at optimal reaction conditions thus increasing the overall hydrocarbon product yield. The alkane activation or first-stage is operated at a higher temperature than the second-stage since light alkanes are much less reactive than light olefins. Since aromatization of olefins is more efficient at higher pressure, the second-stage is maintained at a higher pressure than the first-stage. Further, fixed-bed catalysts are used in each of the first-stage and the second-stage. 1. A method for converting light hydrocarbon feedstock to produce liquid transportation fuels , the method comprising:contacting a light hydrocarbon feedstock comprising at least one C3-C5 alkane with a first fixed-bed catalyst in a first-stage conversion reactor to produce a first-stage effluent, wherein reaction conditions in the first-stage conversion reactor comprise a first temperature in a range from 400 degrees Celsius to 650 degrees Celsius and a first pressure in a range from 0 psig to 100 psig;separating the first-stage effluent in a first separator to produce a first condensed liquid hydrocarbon comprising at least five carbon atoms, and a gas phase product comprising at least one C2-C4 olefin;contacting the gas phase product with a second fixed-bed catalyst in a second-stage conversion reactor to produce a second-stage effluent, wherein reaction conditions in the second-stage conversion reactor comprise a second temperature lower than the first temperature and in a range from 200 degrees Celsius to 400 degrees Celsius and a second pressure in a range from 0 psig to 500 psig; andseparating the second-stage effluent in a second separator to produce a second condensed ...

FIXED BED RADIAL FLOW REACTOR FOR LIGHT PARAFFIN CONVERSION

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

Oligomerization Process

A process for oligomerizing an olefin feedstock to produce an olgiomerization product, a method for analysing an oligomerization product, and an oligomerization product are disclosed. Preferably, the process comprises contacting the olefin feedstock with an oligomerization catalyst under effective oligomerization conditions, wherein the olefin feedstock comprises at least 50 wt % of one or more Colefins, based on the weight of the olefins in the olefin feedstock, and wherein the oligomerization catalyst comprises a crystalline molecular sieve, such as an intermediate pore size crystalline molecular sieve or a large pore size crystalline molecular sieve. 1. A process for oligomerizing an olefin feedstock to form an oligomerization product , wherein the process comprises contacting the olefin feedstock with an oligomerization catalyst under effective oligomerization conditions;{'sub': '6', 'wherein, the olefin feedstock comprises at least 50 wt % of one or more Colefins, based on the weight of the olefins in the olefin feedstock;'}and wherein, the oligomerization catalyst comprises a crystalline molecular sieve.2. The process according to claim 1 , wherein the crystalline molecular sieve comprises at least one of an intermediate pore size crystalline molecular sieve having 10-membered ring pores claim 1 , or a large pore size crystalline molecular sieve having 12-membered ring pores.3. The process according to claim 2 , wherein the intermediate pore size crystalline molecular sieve claim 2 , if present claim 2 , is a zeolite having a structure type selected from the list consisting of AEL claim 2 , MFI claim 2 , MFS claim 2 , MEL claim 2 , MRE claim 2 , MTW claim 2 , MWW claim 2 , EUO claim 2 , MTT claim 2 , HEU claim 2 , FER claim 2 , and TON claim 2 , and the large pore size crystalline molecular sieve claim 2 , if present claim 2 , is a zeolite having a structure type selected from the list consisting of LTL claim 2 , VFI claim 2 , MAZ claim 2 , MEI claim 2 , FAU ...

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

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

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

The present disclosure provides petrochemical processing methods and systems, including ethylene conversion processes and systems, for the production of higher hydrocarbon compositions, for example liquid hydrocarbon compounds, with reduced amount of unsaturated hydrocarbons. 1. A method for generating hydrocarbon compounds with eight or more carbon atoms (C compounds) , comprising:{'sub': 2+', '2+', '3+, '(a) directing a feed stream comprising unsaturated C hydrocarbon compounds into an oligomerization unit that permits at least a portion of said unsaturated C hydrocarbon compounds to react in an oligomerization process to yield an effluent comprising unsaturated C hydrocarbon compounds; and'}{'sub': 3+', '8+, '(b) directing at least a portion of said effluent from said oligomerization unit and a stream comprising isoparaffins into an alkylation unit downstream of and separate from said oligomerization unit, which alkylation unit permits at least a portion of said unsaturated C hydrocarbon compounds and said isoparaffins to react in an alkylation process to yield a product stream comprising said C compounds.'}2. The method of claim 1 , further comprising: directing methane and an oxidizing agent into an oxidative coupling of methane (OCM) unit that facilitates an OCM reaction to generate an OCM product stream comprising ethylene (CH) claim 1 , and wherein at least a portion of said feed stream is provided by the OCM product stream.3. The method of claim 1 , wherein the oligomerization unit comprises a dimerization unit and the oligomerization process comprises a dimerization process claim 1 , and wherein the dimerization process operates at a temperature of 20° C. to 200° C. and a pressure of 100 psia to 400 psia.4. The method of claim 1 , wherein the product stream is an alkylate stream comprising an alkylate product comprising saturated C hydrocarbon compounds claim 1 , isomers thereof claim 1 , or both saturated C hydrocarbon compounds and isomers thereof.5. The ...

ISOMERIZATION AND CATALYTIC ACTIVATION OF PENTANE-ENRICHED HYDROCARBON MIXTURES

The present disclosure relates to processes that catalytically convert a hydrocarbon feed stream predominantly comprising both isopentane and n-pentane to yield upgraded hydrocarbon products that are suitable for use either as a blend component of liquid transportation fuels or as an intermediate in the production of other value-added chemicals. The hydrocarbon feed stream is isomerized in a first reaction zone to convert at least a portion of the n-pentane to isopentane, followed by catalytic-activation of the isomerization effluent in a second reaction zone with an activation catalyst to produce an activation effluent. The process increases the conversion of the hydrocarbon feed stream to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. Certain embodiments provide for further upgrading of at least a portion of the activation effluent by either oligomerization or alkylation. 1. A method for converting a feed stream comprising pentanes to produce a liquid transportation fuel , comprising:a. providing a hydrocarbon feed stream comprising at least 50 wt. % pentanes, including both n-pentane and isopentane;b. contacting the hydrocarbon feed stream with one or more isomerization catalysts in a first reaction zone that is maintained at a temperature and a pressure that facilitates the isomerization of at least a portion of the n-pentane in the hydrocarbon feed stream to isopentane, thereby producing an isomerization effluent characterized by an increased ratio of isopentane to n-pentane relative to the hydrocarbon feed stream;c. contacting the isomerization effluent with an activation catalyst in a second reaction zone that is maintained at a temperature and pressure that facilitates at least one reaction selected from dehydrogenation, cracking and aromatization, thereby converting at least a portion of hydrocarbons present in the isomerization effluent to produce an activation effluent comprising olefins containing from two to five carbon ...

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

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

METHOD FOR PRODUCING AN AROMATIC HYDROCARBON WITH AN OXYGENATE AS RAW MATERIAL

A method for producing an aromatic hydrocarbon with an oxygenate as raw material, includes: i) reacting an oxygenate in at least one aromatization reactor to obtain an aromatization reaction product; ii) separating the aromatization reaction product to obtain a gas phase hydrocarbons flow X and a liquid phase hydrocarbons flow Y; iii) after removing gas and/or a part of the oxygenate from the gas phase hydrocarbons flow X, a hydrocarbons flow X containing a non-aromatic hydrocarbon is obtained; or after removing gas and/or a part of the oxygenate from the gas phase hydrocarbons flow X, a reaction is conducted in another aromatization reactor and a separation is conducted to obtain a flow X containing a non-aromatic hydrocarbon and a flow X containing an aromatic hydrocarbon. The flows are further treated. 1. A method for producing an aromatic hydrocarbon with an oxygenate as raw material , comprisingi) reacting an oxygenate in at least one aromatization reactor to obtain an aromatization reaction product;ii) separating the aromatization reaction product through a separation unit A, to obtain a gas phase hydrocarbons flow X and a liquid phase hydrocarbons flow Y;{'b': '1', 'iii) after removing gas and/or a part of the oxygenate from the gas phase hydrocarbons flow X through a separation unit B, a hydrocarbons flow X containing a non-aromatic hydrocarbon is obtained; or'}after removing gas and/or a part of the oxygenate from the gas phase hydrocarbons flow X through a separation unit B,{'b': 2', '3, 'a reaction is conducted in another aromatization reactor and a separation is conducted through a separation unit A, to obtain a flow X containing a non-aromatic hydrocarbon and a flow X containing an aromatic hydrocarbon;'}{'b': '3', 'iv) after combining the liquid phase hydrocarbons flow Y and optionally the flow X containing an aromatic hydrocarbon, a mixed hydrocarbons flow M of an aromatic hydrocarbon having less than or equal to 7 carbon numbers and a flow N of the ...