ДИЦИКЛОПРОПАНИРОВАННЫЙ 5-ВИНИЛ-2-НОРБОРНЕН И СПОСОБ ЕГО ПОЛУЧЕНИЯ

Изобретение относится к органическому синтезу и более конкретно к способу получения дициклопропанированного 5-винил-2-норборнена, включающему растворение 5-винил-2-норборнена в органическом растворителе, добавление соли палладия (II), охлаждение полученного раствора до (-15)-(-20)°С, добавление раствора диазометана к раствору 5-винил-2-норборнена и перемешивание полученного раствора в течение 2-2.5 часов при этой температуре, затем нагревание раствора до комнатной температуры и перемешивание в течение 20-24 часов, фильтрацию полученной реакционной смеси и последующее упаривание в вакууме 40-50 мм рт.ст. при комнатной температуре с удалением органического растворителя и получением целевого продукта - дициклопропанированного 5-винил-2-норборнена. Технический результат - получение целевого продукта с выходом, близким к количественному - до 97-99%. 2 з.п. ф-лы, 2 ил., 2 табл., 4 пр.

Способ производства изопрена из изобутилена и формальдегида без выделения промежуточных продуктов

Изобретение относится к способу производства изопрена из изобутилена и формальдегида без выделения промежуточных продуктов в присутствии водорастворимых кислот, например ортофосфорной, с традиционно используемыми схемами разделения конечных продуктов синтеза: изобутилена, изопрена, пиранов и смол. Способ характеризуется тем, что смешивают раствор формальдегида в воде, содержащий 20-30% мас. формальдегида, до 3% мас. ортофосфорной кислоты, с изобутиленом с концентрацией не ниже 99,5% мас., подаваемым в соотношении 1,3-1,7 моль на 1 моль формальдегида; подают полученную смесь в реакторы, три из которых - трубчатые с интенсивным теплосъёмом и три или более - аппараты с мешалкой и охлаждающей рубашкой для глубокого исчерпывания формальдегида до 0,7-0,5% мас., в которых взаимодействие изобутилена и формальдегида протекает в жидкой фазе при температуре 95-98°С и избыточном давлении 20-22 кг/см2; распыляют все продукты реакции после жидкофазного синтеза в реакторах вместе с непрореагировавшими ...

СПОСОБ ПОЛУЧЕНИЯ 2,6-ДИЦИКЛОГЕКСИЛНАФТАЛИНА

Сущность изобретения: получение 2,6-дициклогексилнафталина (2,6-ДУГН) алкилированием нафталина. Алкилирующий агент: циклогексен. Cl- или В-циклогексан, циклогексанол. Условия: максимальная температура алкилирования 140 - 220oС, максимальное давление 5 - 30 атм. Катализатор: цеолит типа фожазита, имеющий открытые поры выше 6,7 массовое отношение SiO2/Al2O3 выше 2,5 и остаточное содержание ионов щелочных металлов менее 3 мас.%, преимущественно в виде суспензии в реакционной среде. Реакционная среда содержит растворитель нафталина, алкилирующий агент и алкилированные нафталины. Из полученного алкилата 2,6-ДУГН выделяют кристаллизацией, преимущественно частичным испарением растворителя. Оставшуюся некристаллизированную часть подвергают дезалкилированию при максимальной температуре 260 - 350oС и максимальном давлении 10 - 60 атм в присутствии катализатора вышеуказанного типа. Регенирированный нафталин возвращают на алкилирование. 8 з. п. ф-лы, 3 ил., 1 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 ...

Verfahren zur Herstellung von ª†-arylsubstituierten gesaettigten aliphatischen Mono- oder Polycarbonsaeureestern oder der freien Saeuren

Process for the synthesis of arylfluorenes and analogues thereof

ZEOLITE CATALYST COMPOSITION AND USE THERE OF IN TRANSALKYLATION OF ALKYLAROMATIC HYDROCARBONS

... 1337843 Zeolite composition UNIVERSAL OIL PRODUCTS CO 19 April 1971 [16 March 1970] 24161/71 Heading C1A [Also in Divisions B1 and C5] A catalyst composition comprises alumina and from 50-90 wt. per cent (w.r.t. the composition) of a zeolite of mordenite crystal structure, said composition being characterized by its preparation which comprises (a) heating an amorphous SiO 2 /Al 2 O 3 composite (SiO 2 : Al 2 O 3 in a ratio 12 : 1-30 : 1) at 140-250‹ C. with sufficient of an aqueous solution containing alkali metal ions to provide an alkali metal : Al atomic ratio of 1À5 : 1-3À5 : 1 yielding a mordenite zeolite having substantially the same SiO 2 /Al 2 O 3 ratio ast he initial composition and (b) heating said zeolite in an alumina sol, separating off excess sol, gelling the sol and ageing the resulting composition in an alkaline medium for at least 5 hours before washing, drying and calcining. The solution containing alkali metal ions may be aqueous NaOH, the alumina sol may be an AlCl 3 ...

Production of alkylated compounds

PROCEDURE FOR THE PRODUCTION OF CUMOL IS USED WITH THE PRODUCTION OF PHENOL

ON POLYPHENYLMETHANEN BASED COMPOSITIONS, PROCEDURE FOR YOUR PRODUCTION AND YOUR USE AS DIELECTRIC.

PROCEDURE FOR THE PRODUCTION OF A VERB-MOVED BISCYCLOPENTADIENVERBINDUNG

Procedure for the production of aromatic connections with Stilbenkonfiguration (EN)

COMPOSITION OF DIPHENYLMETHANEMETHYL AND BENZYL DERIVATIVES, ITS APPLICATION AS DIELECTRIC

La présente invention concerne une composition à base de benzyltoluène, (méthylbenzyl)toluène, benzylxylène, (méthylbenzyl)xylène pouvant éventuellement contenir leurs dérivés benzylés ou méthylbenzylés. Cette composition est préparée par chloration d'un mélange de xylène et de toluène dans lequel on ajoute ensuite un catalyseur de FRIEDEL et CRAFTS. Après distillation du toluène et du xylène en excès, on obtient un liquide à usage diélectrique qui présente l'avantage de rester liquide jusqu'à de très basses températures.

Verfahren zur Herstellung von in 4,6- und 8-Stellung substituierten Azulenen

Verfahren zur Herstellung aromatischer, Äthylendoppelbindungen enthaltender Verbindungen

Sulphonated distyryl benzenes prodn - by condensing 4-methylstilbenes and sulphoanils in presence of strong base

Preparing 1,4-distyrylbenzenes (I) comprises reacting a 4-methyl stilbene (II) with anil (III) in presence of a strongly basic alkali cpd. in a strongly polar neutral-to-basic org. solvent. (rings, A, B, and C are opt. substd. by nonchromophoric gps. and 1 of A and C has a SO3M substit M=H or salt-forming cation; ring A can also represent naphthalene; Ar=opt. substd. aryl). Yields of (I) are food. (I) are optical brighteners for high mol. wt. org. materials e.g. for incorporation into detergent compsns or spinning melts.

Disubstituted ethanes

Compounds of the formula in which R<2> is one of the groups -R<3>, -OR<3>, -CO-R<3>, -CO-OR<3> and -O-CO-R<3>, R<1> and R<3> are straight-chain alkyl groups having 1 to 12 carbon atoms, and n is one of the numbers 1 and 2, their preparation, mixtures which contain such compounds, and the use in electro-optical devices are described. The novel compounds of the formula I are particularly useful as components in liquid-crystal mixtures and for the most part themselves have liquid-crystalline properties.

METHOD OF DIRECT OF PRODUCING P - XYLENE FROM SYNTHESIS - GAS AND AROMATIC HYDROCARBON

A high-performance toluene side-chain alkylation catalyst preparation and application thereof

CYCLOPROPANATION

... in which X is a nucleofuge selected from halides and pseudohalides and Y is an electrofuge selected from boranes and borates, in the presence of a metal catalyst complex selected from those useful for catalytic cyclopropanation and those useful for catalyzing Heck coupling. The method provides a particularly easy and non-hazardous method of cyclopropanation.

Synthesis of liquid fuels and chemicals from oxygenated hydrocarbons

Processes and reactor systems are provided for the conversion of oxygenated hydrocarbons to hydrocarbons, ketones and alcohols useful as liquid fuels, such as gasoline, jet fuel or diesel fuel, and industrial chemicals. The process involves the conversion of mono-oxygenated hydrocarbons to aromatics and gasoline range hydrocarbons where the oxygenated hydrocarbons are derived from biomass.

Method for producing aryl, heteroaryl, or alkenyl-substituted unsaturated hydrocarbon

The present invention relates to a method for producing aryl-, heteroaryl- or alkenyl-substituted unsaturated hydrocarbons, containing: reacting aryl halides, heteroaryl halides or alkenyl halides with alkynes or alkenes in the presence of a palladium catalyst to obtain a crude product, and subsequently distillatively purifying the crude product in the presence of a compound having at least one NCS group.

Способ получения 1-[2-(2,2-диметилциклопропил)этил]-1,1'-бициклопропана путем циклопропанирования мирцена

Предлагаемое изобретение относится к органической химии, конкретно к способу получения 1-[2-(2,2-диметилциклопропил)этил]-1,1'-бициклопропана, представляющего интерес в качестве высокоэнергетического соединения, перспективного синтетического углеводородного горючего. Способ получения 1-[2-(2,2-диметилциклопропил)этил]-1,1'-бициклопропана (1) осуществляют путем циклопропанирования мирцена и характеризуется тем, что мирцен подвергают взаимодействию с диазометаном (CH2N2) в присутствии Et2AlCl при мольном соотношении мирцен : CH2N2 : Et2AlCl = 1:(3-5):(3-5), в среде хлористого метилена, в атмосфере аргона при 20-23°С и атмосферном давлении в течение 6 ч. Выход полициклического углеводорода (1) составляет 85-93%. 1 табл.

СПОСОБ ПОЛУЧЕНИЯ АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ

Представлен способ получения ароматических углеводородов с применением оксигената в качестве исходного материала. Используют: реакцию с участием оксигената в одном реакторе ароматизации, получение и разделение продукта реакции ароматизации на сепарационной установке А, в которой осуществляют охлаждение, промывку щелочью и/или водой, получение потока газообразных углеводородов X и потока жидких углеводородов Y; получение неароматических углеводородов X1 после удаления газа и/или части оксигената на сепарационной установке В, в которой осуществляется короткоцикловая безнагревная адсорбция, ректификация (разгонка) и/или адсорбция; получение Х2, содержащего неароматические углеводороды, и потока Х3, содержащего ароматические углеводороды, после удаления газа, части оксигената из потока Х на сепарационной установке В, на которой осуществляется короткоцикловая безнагревная адсорбция, ректификация и/или адсорбция, реакцией в другом реакторе ароматизации и разделением на сепарационной установке ...

Каталитическая композиция и способ ее применения для алкилирования ароматических углеводородов спиртами или смесями спиртов и олефинов

Настоящее изобретение относится к каталитической композиции для алкилирования ароматических углеводородов, таких как бензол или толуол, алифатическими спиртами, содержащими от 1 до 8 атомов углерода, содержащая: цеолит типа MTW, щелочные металлы, которые являются смесью ионов натрия и ионов калия, причем количество натрия составляет от 5 до 40 частей на млн., количество калия составляет от 5 до 80 частей на млн., общее количество щелочных металлов в каталитической композиции составляет менее 200 частей на млн. (0,02 мас.%) относительно общей массы каталитической композиции и молярное отношение SiO/AlOв указанном цеолите типа MTW составляет от 20 до 95. Также описан способ алкилирования ароматических углеводородов, таких как бензол или толуол, в присутствии такой каталитической композиции. Технический результат – разработка каталитической композиции с пониженным содержанием катионов щелочных металлов, обладающей оптимальными характеристиками и сроком службы и, как следствие, производительностью ...

СПОСОБ ПЕРЕРАБОТКИ ФРАКЦИИ ВЫСОКОКИПЯЩИХ ПРОДУКТОВ И ПИРАНОВОЙ ФРАКЦИИ

Изобретение относится к способу переработки фракции высококипящих продуктов и пирановой фракции, являющихся побочными продуктами процесса получения изопрена из изобутилена и формальдегида, путем смешения исходных продуктов с водяным паром, включающий предварительное испарение и нагрев пирановой фракции до температуры 400-480°С, с последующим разложением обработанных исходных продуктов в секционном реакторе с алюмосиликатсодержащим катализатором при повышенной температуре. Способ характеризуется тем, что процесс разложения проводят при температуре в реакторе 430-550°С с раздельной подачей исходных продуктов в реактор: фракцию высококипящих продуктов подают в первую секцию реактора, а пирановую фракцию - во вторую секцию реактора. Предлагаемый способ позволяет повысить конверсию тяжелого остатка до 88,1%, снизить расход пара. 1 табл., 2 пр.

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

Изобретение относится к устройству и способу получения пара-ксилола (РХ) и совместного получения низших олефинов. Представлен реактор с турбулентным кипящим слоем для получения пара-ксилола и совместного получения низших олефинов из метанола и/или диметилового эфира и бензола, причем указанный реактор с турбулентным кипящим слоем включает распределитель первого сырья для реактора и множество распределителей второго сырья для реактора, и распределитель первого сырья для реактора и множество распределителей второго сырья для реактора расположены последовательно снизу вверх в реакционной зоне реактора с турбулентным кипящим слоем; при этом количество распределителей второго сырья для реактора составляет от 2 до 10, при этом реактор с турбулентным кипящим слоем включает первый сепаратор твёрдой и газовой фаз реактора, при этом первый сепаратор твёрдой и газовой фаз реактора расположен в зоне разбавленной фазы или за пределами корпуса реактора, при этом первый сепаратор твердой и газовой фаз ...

УСТРОЙСТВО И СПОСОБ ПОЛУЧЕНИЯ ПАРА-КСИЛОЛА И СОВМЕСТНОГО ПОЛУЧЕНИЯ НИЗШИХ ОЛЕФИНОВ ИЗ МЕТАНОЛА И/ИЛИ ДИМЕТИЛОВОГО ЭФИРА И БЕНЗОЛА

Изобретение относится к реактору с быстрокипящим слоем для получения пара-ксилола и совместного получения низших олефинов из метанола и/или диметилового эфира и бензола, где нижняя часть реактора с быстрокипящим слоем представляет собой реакционную зону и верхняя часть реактора с быстрокипящим слоем представляет собой зону разбавленной фазы. При этом указанный реактор с быстрокипящим слоем включает корпус реактора, распределитель первого сырья для реактора и множество распределителей второго сырья для реактора, при этом и указанный распределитель первого сырья для реактора и указанное множество распределителей второго сырья для реактора расположены последовательно снизу вверх в реакционной зоне. Также указанный реактор с быстрокипящим слоем включает первый сепаратор твердой и газовой фаз реактора, при этом указанный первый сепаратор твердой и газовой фаз реактора расположен в зоне разбавленной фазы или за пределами корпуса реактора. Причем указанный первый сепаратор твердой и газовой фаз ...

СПОСОБ И УСТАНОВКА ДЛЯ ПРОИЗВОДСТВА ИЗОПРЕНА (ВАРИАНТЫ)

Изобретение относится к двум вариантам способа получения изопрена путем взаимодействия изобутилена и формальдегида и/или веществ являющихся их источниками. Один из вариантов включает синтез триметилкарбинола, синтез диметилдиоксана с выделением побочных продуктов, синтез изопрена при температуре 150-200°С и давлении 0,6-1,7 МПа в присутствии кислотного катализатора, с последующим разложением побочных продуктов и выделением и очисткой изопрена, отличающийся тем, что в качестве источника изобутилена используют С4 фракцию пиролиза и/или крекинга, содержащую до 30 мас.% бутена-1 и до 10 мас.% бутена-2, полученный изопрен дополнительно очищают от пипериленов известным способом. Изобретение содержит технические решения, позволяющие расширить сырьевую базу при получении изопрена жидкофазным и парофазным способом при сохранении высокого качества целевого продукта-изопрена. 2 н.п. ф-лы, 2 ил., 2 пр.

СПОСОБ ПОЛУЧЕНИЯ 1,3-БУТАДИЕНА

Предложен способ получения бутадиена-1,3, включающий взаимодействие формальдегидсодержащего сырья с пропиленом в присутствии твердофазного катализатора в условиях газофазной конденсации при атмосферном давлении. В качестве катализатора используют гетерополикислоту, выбранную из ряда: 12-фосфорвольфрамовая, 12-вольфрамокремниевая, 12-фосформолибденовая, содержащуюся в количестве от 5 до 99 мас. % на пористом носителе. Технический результат – упрощение процесса за счет его проведения в одну стадию, а также повышение выхода целевого продукта и селективности образования бутадиена при высокой стабильности работы катализатора во времени. 4 з.п. ф-лы, 1 табл., 20 пр.

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

Изобретение относится к устройству и способу получения пара-ксилола (РХ) и совместного получения низших олефинов. Представлен реактор с турбулентным кипящим слоем для получения пара-ксилола и совместного получения низших олефинов из метанола и/или диметилового эфира и бензола, причем указанный реактор с турбулентным кипящим слоем включает распределитель первого сырья для реактора и множество распределителей второго сырья для реактора, и распределитель первого сырья для реактора и множество распределителей второго сырья для реактора расположены последовательно снизу вверх в реакционной зоне реактора с турбулентным кипящим слоем; при этом количество распределителей второго сырья для реактора составляет от 2 до 10, при этом реактор с турбулентным кипящим слоем включает первый сепаратор твёрдой и газовой фаз реактора, при этом первый сепаратор твёрдой и газовой фаз реактора расположен в зоне разбавленной фазы или за пределами корпуса реактора, при этом первый сепаратор твердой и газовой фаз ...

СПОСОБ РАЗДЕЛЕНИЯ КЛАСТЕРОВ ЧАСТИЦ АЛМАЗА

... 1. Способ разделения кластеров частиц алмаза, диаметр которых не превышает 1,0 мм, на отдельные частицы и(или) на кластеры меньших размеров, содержащие меньшее количество алмазных частиц, включающий следующие стадии:(a) перемешивание кластеров частиц алмаза по меньшей мере с одним ненасыщенным органическим соединением, находящимся в жидком агрегатном состоянии, или с раствором по меньшей мере одного ненасыщенного органического соединения по меньшей мере в одном растворителе для получения реакционной смеси, и(b) сообщение кластерам частиц алмаза кинетической энергии с помощью механических средств для разрушения кластеров частиц алмаза до получения в среде реакционной смеси отдельных алмазных частиц и(или) кластеров меньших размеров, содержащих меньшее количество алмазных частиц, с образованием алмазных частиц с ненасыщенными углеродными связями на поверхности и с реагированием упомянутого по меньшей мере одного органического или неорганического соединения по меньшей мере с некоторыми из ...

Способ получения кристаллического металлосиликата

СПОСОБ ПОЛУЧЕНИЯ КРИСТАЛЛИЧЕСКОГО МЕТАЛЛОСИЛИКАТА смешением растворов солен металлов с соединением кремния, выдерживанием при гидротермальных условиях и отделением от маточной жидкости, о т л и ч а rant и и с я тем, что, с целью получения кристаллического металлосиликата с высокой каталитической активностью в качестве исходных солей металлов используют нитрат или окись натрия или калия и/или нитрат или сульфат железа с добавлением в раствор четвертичного aNtMOHHeBoro основания и в качестве соединения кремния используют двуокись кремния или жидкое стекло при следующем молярном отношении солей в пересчете на окислы: или KjO: четвертичное аммони :пое основание0,05-1,5 (Л Четвертичное аммониевое основание: SiO, 0,05-0,4 20-600 SiOj:Ре20з SiO, 6-60 Н,0 ...

Method for separation of diamond particle clusters

A method for the separation of diamond particle clusters into discrete diamond particles and/or into smaller diamond particle clusters comprising fewer diamond particles is disclosed. The diamond particle clusters are combined with at least one liquid phase organic or inorganic compound, or with a solution of at least one organic or inorganic compound in at least one solvent to form a reaction mixture. Mechanical means (e.g. shaking, stirring, milling with beads or sonication) are then used to separate the diamond particle clusters into discrete diamond particles and/or into smaller clusters within the reaction mixture producing diamond particles with free bonding sites on the surface of the diamond particles. The at least one organic or inorganic compound (e.g. an alkene such as undecene) then reacts with these free carbon bonding sites present on the diamond particle surface. The surfaces of the diamond particles are functionalised by the reaction with the organic or inorganic compounds ...

Improvements in or relating to organic compounds

Diakyl pentacene derivatives with c-alkyne solubilising units and their applications as small molecule organic semiconductors

COMPOSITIONS OF XYLENE GROUPINGS ABSTENTIONS POLYARYLALKANOLIGOMEREN AND PROCEEDING TO THEIR PRODUCTION.

CATALYTIC ALKYLATION OF AROMATIC ALKYLBENZENE

PROCESS FOR CONVERSION OF METHANE TO HIGHER HYDROCARBONS, INCLUDING LIQUID FUELS

Aspects of the invention are associated with the discovery of processes for converting methane (CH4), present in a methane-containing feedstock that may be obtained from a variety of sources such as natural gas, to higher hydrocarbons (e.g., C4+ hydrocarbons) such as gasoline, diesel fuel, or jet fuel boiling-range hydrocarbons, which may optionally be separated (e.g., by fractionation) for use as transportation fuels, or otherwise as blending components for such fuels. Particular aspects of the invention are associated with advantages arising from maintaining reaction conditions that improve the yield of C4+ hydrocarbons. Further aspects relate to the advantages gained by integration of the appropriate reactions to carry out the methane conversion, with downstream separation to recover and recycle desirable components of the reaction effluent, thereby improving process economics to the extent needed for commercial viability.

CARBOHYDRATE ROUTE TO PARA-XYLENE AND TEREPHTHALIC ACID

Preparation method of tail end isoprene compound cyclopropanation

PRODUCTION D'ALKYLBENZENES

L'invention concerne l'industrie chimique. Elle a pour objet un procédé d'alkylation d'un hydrocarbure aromatique par contact avec un agent d'alkylation dans des conditions convenables et en présence d'un catalyseur comprenant de la zéolite upsilon -1. Le procédé de l'invention est préféré pour la production d'hydrocarbures aromatiques avec un meilleur rendement résultant de l'alkylation de composés moins utiles en produits fort intéressants.

Autoclave with triple wall made from conical tubes - for direct synthesis of hydrocarbon(s) from coal, liq. hydrocarbon(s) and hydrogen

Synthesis of liquid fuels and chemicals from oxygenated hydrocarbons

Processes and reactor systems are provided for the conversion of oxygenated hydrocarbons to hydrocarbons, ketones and alcohols useful as liquid fuels, such as gasoline, jet fuel or diesel fuel, and industrial chemicals. The process involves the conversion of mono-oxygenated hydrocarbons, such as alcohols, ketones, aldehydes, furans, carboxylic acids, diols, triols, and/or other polyols, to C4+ hydrocarbons, alcohols and/or ketones, by condensation. The oxygenated hydrocarbons may originate from any source, but are preferably derived from biomass.

Cyclopropanation

A method of preparing a cyclopropane ring-bearing compound of the formula I in which R1and R2are independently selected from C1-C10alkyl, optionally substituted, or R1and R2, together with the bonds linking them to the cyclopropane ring, form a monocyclic or bicyclic ring system, which may comprise at least one hetero-atom, comprising the reaction of a compound of formula II R1—CH═CH—R2 II in which R1and R2have the significances hereinabove defined, with a compound of formula III X—CH2—Y III in which X is a nucleofuge selected from halides and pseudohalides and Y is an electrofuge selected from boranes and borates, in the presence of a metal catalyst complex selected from those useful for catalytic cyclopropanation and those useful for catalyzing Heck coupling. The method provides a particularly easy and non-hazardous method of cyclopropanation.

SYNTHESIS OF LIQUID FUELS AND CHEMICALS FROM OXYGENATED HYDROCARBONS

Processes and reactor systems are provided for the conversion of oxygenated hydrocarbons to hydrocarbons, ketones and alcohols useful as liquid fuels, such as gasoline, jet fuel or diesel fuel, and industrial chemicals. The process involves the conversion of mono-oxygenated hydrocarbons, such as alcohols, ketones, aldehydes, furans, carboxylic acids, diols, triols, and/or other polyols, to C4+ hydrocarbons, alcohols and/or ketones, by condensation. The oxygenated hydrocarbons may originate from any source, but are preferably derived from biomass.

A PROCESS FOR THE PREPARATION OF ISOMERS OF XYLENE

The present disclosure relates to a process for the preparation of isomers of xylene. The process includes method step of contacting an activated alkylation catalyst composite with toluene and methanol in the presence of an inert gas, at a temperature of 300 to 500° C. to obtain isomers of xylene. The alkylation catalyst composite used in accordance with the present disclosure comprises a molecular sieve loaded with at least one metal ion. The metal loaded on the molecular sieve is at least one alkali earth metal selected from the group consisting of barium, strontium, magnesium and calcium.

СПОСОБ АЛКИЛИРОВАНИЯ АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ СПИРТАМИ C-C

Изобретение относится к способу алкилирования ароматических углеводородов при помощи алифатических спиртов, содержащих от 1 до 8 атомов углерода. Способ включает в себя подачу углеводорода и спирта с крышки корпуса реактора с неподвижным слоем, функционирующего в режиме "капельного потока", содержащего, по меньшей мере, один слой катализатора, включающего в себя цеолит, выбранный из цеолитов со средними порами и цеолитов с большими порами, причем в реакторе алкилирования ароматический углеводород и алифатический спирт находятся в газовой фазе, а продукты алкилирования находятся в жидкой фазе. Также изобретение относится к способу получения фенола. Настоящий способ позволяет увеличить выход целевых продуктов и снизить выход побочных. 2 н. и 11 з.п. ф-лы, 4 пр.

РЕАКТОР ДЛЯ КАТАЛИТИЧЕСКОЙ ПАРОВОЙ И ПАРОУГЛЕКИСЛОТНОЙ КОНВЕРСИИ УГЛЕВОДОРОДОВ

Изобретение относится к реактору для каталитической паровой и пароуглекислотной конверсии углеводородов, содержащему цилиндрический корпус с эллиптическим дном, закрытый крышкой, при этом во внутренней полости корпуса вдоль цилиндрической его части закреплены на крышке множество вертикальных нагревательных труб байонетного типа, оборудованных горелками и штуцерами подвода топлива, окислителя и штуцером отвода дымовых газов, которые установлены вдоль цилиндрической части. Реактор характеризуется тем, что байонетные трубы выполнены из керамического материала, а горелки расположены внутри байонетных труб. Использование предлагаемого реактора обеспечивает более глубокую переработку метана за счет повышения верхней границы температуры каталитического процесса. 4 ил.

СПОСОБ АЛКИЛИРОВАНИЯ АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ СПИРТАМИ С-С

... 1. Способ алкилирования ароматических углеводородов при помощи алифатических спиртов, содержащих от 1 до 8 атомов углерода, который включает в себя подачу углеводорода и спирта с крышки корпуса реактора с неподвижным слоем, функционирующего в режиме "капельного потока", содержащего, по меньшей мере, один слой катализатора, включающего в себя цеолит, выбранный из цеолитов со средними порами и цеолитов с большими порами.2. Способ по п. 1, проводимый непрерывно, который включает в себя:a. Смешивание в жидкой фазе, по меньшей мере, одного ароматического углеводорода (А), спирта, содержащего от 1 до 8 атомов углерода (В) и рециркулируемого потока (С), приходящего от секции выгрузки из реактора алкилирования,b. Подачу полученной конечной смеси, заранее нагретой до температуры реакции, в крышку реактора алкилирования с неподвижным слоем, функционирующего в режиме "капельного потока", содержащего, по меньшей мере, один слой катализатора, включающий в себя цеолит, выбранный из цеолитов со средними ...

Способ получения ароматических углеводородов с @ -с @

Verfahren zur Herstellung einer methylenverbrückten Biscyclopentadienverbindung

Process for the synthesis of arylfluorenes and analogues thereof

A process is provided for the synthesis of a compound of formula (1) wherein m=0 or 1; n and p are 0 or 1 to 4; X is a single bond, O,S or NH; and R<1> - R<4> are as defined in claim 1.

Diesters and triesters of aromatic carboxylic acids, salts thereof and polyvinyl chloride resin compositions plasticized with the esters

The invention comprises compounds of formula C6H5CQ3, wherein the benzene ring may be substituted with 1-3 C1- 4-alkyl groups and/or Cl atoms, Q is C1- 4-alkyl or -CH2CHXCO2Z X is H or C1- 4-alkyl and Z is H or C1- 9-alkyl, not more than one Q being alkyl. Such compounds may be prepared by the method of Specification 990,083 or, where Z is, e.g., C4- 9-alkyl, by respectively esterifying or transesterifying the appropriate acid or lower alkyl ester. Specified compounds which may be thus produced are octyl 4-phenyl-2,4,6-trimethylpimelate, 2-ethylhexyl 4-methyl-4-p-tolylpimelate and butyl 4-(2-carbobutoxyethyl) -4-p-tolylpimelate.ALSO:Polyvinyl chloride is plasticized with compounds of formula C6H5CQ3, wherein the benzene ring may be substituted with 1-3 C1-4-alkyl groups and/or Cl atoms, Q is C1-4-alkyl or -CH2CHXCO2Z, X is H or C1-4-alkyl and Z is C1-9 alkyl, not more than one Q being alkyl. Preferred compounds are octyl 4-phenyl-2,4,6-trimethylpimelate, 2-ethylhexyl 4-methyl-4-p-tolypimelate ...

Improvements in or relating to organic compounds

PROCEDURE FOR THE PRODUCTION OF AN ALKYLATED AROMATIC PRODUCT USING AN ALKYLATING ZEOLITE AND THE ALKYLATING ZEOLITE.

METHYL AND BENZYLE DERIVATIVES OF DIPHENYLMETHAN CONTAINING COMPOSITION AND YOUR USE AS DIELECTRIC.

PROCEDURE FOR THE SUBSTITUTION OF INDENOFLUORENEN

Molecular sieve SSZ-70 composition of matter and synthesis thereof

Synthesis of liquid fuels and chemicals from oxygenated hydrocarbons

Processes and reactor systems are provided for the conversion of oxygenated hydrocarbons to hydrocarbons, ketones and alcohols useful as liquid fuels, such as gasoline, jet fuel or diesel fuel, and industrial chemicals. The process involves the conversion of mono-oxygenated hydrocarbons, such as alcohols, ketones, aldehydes, furans, carboxylic acids, diols, triols, and/or other polyols, to C ...

COMPOSITIONS OF POLYARYLALKANE OLIGOMERS CONTAINING XYLENE UNITS, AND PROCESS FOR THEIR MANUFACTURE

POLYARYLALKANE OLIGOMER COMPOSITIONS AND PROCESS FOR THEIR MANUFACTURE

POLYARYLALKANE OLIGOMER COMPOSITIONS AND PROCESS FOR THEIR MANUFACTURE

METHOD OF PREPARING AN ALKYLATED AROMATIC PRODUCT WITH AN ALKYLATION ZEOLITE AND A DEALKYLATION ZEOLITE

CRYSTALLINE SILICATES

Novel crystalline ferro silicates characterized in thata) they are thermally stable up to temperatures above 600 C;b) after dehydration in vacuo at 400.degree.C they are capable of adsorbing more than 3 %w water at 25.degree.C and saturated water vapour pressure; andc) in the dehydrated form they have the following overall composition, in terms of moles of the oxides: (1.0 ? 0.3)(R)2/nO. ¢a Fe2O3. b A12O3 . c Ga2O3!. y (d SiO2. e GeO2), where R = one or more monovalent or bivalent cations; a ? 0.1; b ?O; c ?O; a + b + c = 1; y ?10; d ?0.1; e ?O; d + e = 1; and n is the valency of R, their preparation and use especially as adsorbing and extracting agents, as drying agent as ion exchanger and as catalyst or catalyst carrier for various catalytic processes, in particular for the ca lytic preparation of aromatic hydrocarbons.

HYBRID MATERIAL, AND METHOD FOR THE PRODUCTION THEREOF

L'invention concerne un matériau sous forme d'un monolithe solide alvéola ire constitué par un polymère d'un oxyde inorganique. Le monolithe comprend des macropores ayant une dimension moyenne dA de 4 .mu.m à 50 .mu.m, des més opores ayant une dimension moyenne d.SIGMA. de 20 à 30 Å et des micropores a yant une dimension moyenne di de 5 à 10 Å, lesdits pores étant interconnecté s. Le polymère d'oxyde inorganique porte des groupements organiques R répond ant à la formule -(CH2)n-R1 dans laquelle 0<=n<=5, et R1 est choisi pa rmi un groupe thiol, un groupe pyrrole, un groupe amino qui porte éventuelle ment un ou plusieurs substituants alkyle, alkylamino ou aryle éventuellement substitué, un groupe alkyle, ou un groupe phényle qui porte éventuellement un substituant R2 de type alkyle. Le matériau est utile comme support de cat alyseur métallique, et pour la décontamination de milieux liquides ou gazeux .

ABSORBER DEMETHANIZER FOR METHANOL TO OLEFINS PROCESS

A process for conversion of methanol to olefins (MTO), including: contacting methanol and air in a methanol-to--olefins reactor; recovering an effluent from the methanol- to-olefins reactor comprising methanol, ethylene, and nitrogen oxides; separating the effluent via one or more reactive distillation and/or distillation stages using a hydrocarbon absorbent to recover a first fraction comprising ethylene and a second fraction comprising methane; wherein the separating comprises operating the one or more extractive distillation and/or distillation stages at temperatures and pressures sufficient to prevent any substantial conversion of nitrogen oxides to N2O3.

PROCESS FOR PREPARING AN ALKYL AROMATIC PRODUCT FROM AN ALKYLATION ZEOLITE AND A DEALKYLATION ZEOLITE

Procédé pour préparer un produit aromatique alkylé (12) par alkylation d'un composé aromatique (1), l'alkylation donnant plusieurs produits aromatiques alkylés, ce procédé étant caractérisé par les points suivants: a) on fait réagir le composé aromatique (1) avec un agent alkylant (2) en présence d'une zéolithe d'alkylation (4) ; b) on sépare par cristallisation le produit aromatique alkylé (12) à partir des produits de l'alkylation ; c) on soumet la partie non cristallisée (13) des produits aromatiques alkylés une déalkylation en présence d'une zéolithe de déalkylation (15) ; d) on recycle le composé aromatique régénéré (1b) pour le faire réagir à nouveau avec l'agent alkylant (2) en présence de la zéolithe d'alkylation (4). Composés aromatiques alkylés (12) obtenus par ce procédé, notamment le dicyclohexyl-2,6 naghtalène.

POLY(PHENYLENEMETHYLENE) COMPOSITIONS; PROCESS FOR PREPARING THE SAME AND THEIR USE AS DIELECTRICS

L'invention concerne une composition à base de deux oligomères A1 et A2: - A1 étant un isomère ou un mélange d'isomères de formule: avec n1 et n2 = 0, 1 et 2 sachant que n1 + n2 est inférieur ou égal à 3 et R représente un hydrogène; - A2 étant un isomère ou un mélange d'isomères de même formule générale que A1 sauf que R représente un méthyle et n1 et n2 sont remplacés par q1 et q2 qui ont respectivement les mêmes significations que n1 et n2, caractérisée en ce que l'un au moins des oligomères A1 et A2 comprend un isomère ayant trois noyaux benzéniques. L'invention concerne également des procédés préférés de préparations de ces mélanges. Ces mélanges possèdent des propriétés diélectriques meilleures que l'art antérieur.

CRYSTALLINE FERRO-SILICATES, PROCESSES TO PREPARE THEM AND THEIR APPLICATIONS

CATALYSTS CONTAINING FERRO-SILICATES CRYSTALLINE, PROCEEDED TO PREPARE THEM AND THEIR APPLICATIONS

PROCEEDED OF PREPARATION OF COMPOSE STILBENIC CONTAINING USEFUL GROUPS SULFO LIKE OPTICAL BLUEINGS

CATALYSTS CONTAINING FERRO-SILICATES CRYSTALLINE, PROCEEDED TO PREPARE THEM AND THEIR APPLICATIONS

METHOD FOR PRODUCING SULFONIC ACID GROUP-CONTAINING CARBONACEOUS MATERIAL, SOLID ACID CATALYST, METHOD FOR PRODUCING ALKYLATION REACTION PRODUCT, AND METHOD FOR PRODUCING OLEFIN POLYMER

Method for producing norbornene derivative

Disclosed is a method for producing a norbornene derivative, wherein a norbornadiene derivative represented by the general formula (3) below is reacted with a bromine compound represented by the general formula (4) below in the presence of palladium and at least one compound selected from the phosphorus compounds represented by the general formulae (1) and (2) below, thereby producing a norbornene derivative represented by the general formula (5) below wherein a substituent represented by Z is in the exo configuration. (In the formula (1), R1, R2, R3 and R4 independently represent a hydrogen atom or the like; and R5 and R6 independently represent a branched saturated hydrocarbon group having 3-10 carbon atoms or the like.) (In the formula (2), R7 represents a branched saturated hydrocarbon group having 3-10 carbon atom.) (In the formula (3), R8, R9, R10, R11 and R12 independently represent a hydrogen atom or the like; l represents an integer of 0 or 1; m represents an integer of 0 or 1; ...

FLUIDIZED BED GAS DISTRIBUTOR, REACTOR USING FLUIDIZED BED GAS DISTRIBUTOR, AND METHOD FOR PRODUCING PARA-XYLENE AND CO-PRODUCING LIGHT OLEFINS

Disclosed are a fluidized bed gas distributor and a fluidized bed reactor, the fluidized bed reactor comprising a first distributor (1) and a second distributor (2), wherein the first distributor (1) is located at the bottom of a fluidized bed, and second distributor (2) is located downstream of a gas from the first distributor (1). Also disclosed is a method for producing a para-xylene and co-producing light olefins, the method comprising the following steps: material stream A enters a reaction zone (3) of a fluidized bed reactor from a first gas distributor (1); material stream B enters the reaction zone (3) of the fluidized bed reactor from a second gas distributor (2); and the reactants are brought into contact with a catalyst in the reaction zone (3) to generate a gas phase stream comprising para-xylene and light olefins.

Способ получения 1-[2-(2,2-диметилциклопропил)этил]-1,1'-бициклопропана

Предлагаемое изобретение относится к органической химии, конкретно, к способу получения 1-[2-(2,2-диметилциклопропил)этил]-1,1'-бициклопропана, представляющего интерес в качестве высокоэнергетического соединения, перспективного синтетического углеводородного горючего. Способ получения 1-[2-(2,2-диметилциклопропил)этил]-1,1'-бициклопропана (1) осуществляют взаимодействием мирцена с дииодметаном (CH2I2) в присутствии металлоорганического соединения. Способ характеризуется тем, что в качестве металлоорганического соединения используют Et3Al, реакцию проводят при мольном соотношении мирцен : CH2I2 : Et3Al = 1:(4-5):(4-5), в среде хлористого метилена, в атмосфере аргона при 20-23°С и атмосферном давлении в течение 6 ч. Выход полициклического углеводорода (1) составляет 80-83%. 1 табл., 1 пр.

СПОСОБ МЕТИЛИРОВАНИЯ БЕНЗОЛА

Изобретение относится к способу метилирования бензола. Способ характеризуется тем, что в качестве метилирующего агента используют диметилдисульфид, процесс осуществляют в присутствии катализатора - высококремнистого цеолита HZSM-5, в газовой фазе при атмосферном давлении, при температуре 250-350°C, времени контакта 1.1-20 с. Технический результат - получение толуола, ксилолов, мезитилена и дурола с использованием альтернативного метилирующего агента - диметилдисульфида. 12 пр., 1 табл.

Способ получения пара-трет-бутилкумола

Изобретение относится к способу получения пара-трет-бутилкумола (ПТБК), который находит применение для получения полимеров и сополимеров для создания композиций красок, покрытий и термореактивных смол. Способ заключается в алкилировании кумола трет-бутиловым спиртом (ТБС). В качестве катализатора используют концентрированную серную кислоту, при этом ее добавляют в реакционную смесь, поддерживая температуру 10-25°С. Далее процесс ведут при температуре 10-35°С в течение 30-180 минут при мольном соотношении кумол:ТБС:H2SO4- 3:1:3. Технический результат: высокие выходы пара-трет-бутилкумола, не содержащего примесей орто- и мета-изомеров. 3 пр.

СИНТЕЗ ЖИДКОГО ТОПЛИВА И ХИМИЧЕСКИХ РЕАКТИВОВ ИЗ КИСЛОРОДСОДЕРЖАЩИХ УГЛЕВОДОРОДОВ

... 1. Способ получения С4+ соединения, включающий: ! обеспечение воды и растворимого в воде кислородсодержащего углеводорода, включающего C1+O1+ углеводород, в водной жидкой фазе и/или паровой фазе, ! обеспечение Н2, ! проведение в жидкой и/или паровой фазе каталитической реакции кислородсодержащего углеводорода с Н2 в присутствии катализатора дезоксигенирования при температуре дезоксигенирования и при давлении дезоксигенирования для получения в реакционном потоке оксигената, включающего С1+О1-3 углеводород, и ! проведение в жидкой и/или паровой фазе каталитической реакции оксигената в присутствии катализатора конденсации при температуре конденсации и при давлении конденсации для получения С4+ соединения, ! где С4+ соединение включает соединение, выбранное из группы, состоящей из С4+ спирта, С4+ кетона, С4+ алкана, С4+ алкена, С5+ циклоалкана, С5+ циклоалкена, арила, конденсированного арила и их смеси. ! 2. Способ по п.1, в котором Н2 включает образованный in situ H2, внешний H2, повторно ...

ГАЗОВЫЙ РАСПРЕДЕЛИТЕЛЬ С КИПЯЩИМ СЛОЕМ, РЕАКТОР С ГАЗОВЫМ РАСПРЕДЕЛИТЕЛЕМ С КИПЯЩИМ СЛОЕМ И СПОСОБ ПОЛУЧЕНИЯ ПАРА-КСИЛОЛА И СОВМЕСТНОГО ПОЛУЧЕНИЯ НИЗШИХ ОЛЕФИНОВ

Группа изобретений относится к газовому распределителю в кипящем слое, реактору, содержащему такой распределитель, и способу получения пара-ксилола и совместного получения низших олефинов. Распределитель содержит первый распределитель, расположенный в нижней части кипящего слоя, и второй распределитель, расположенный по меньшей мере в одной области газового потока на пути его движения из первого распределителя, при этом второй распределитель содержит впускную трубу, микропористую трубу и впускную кольцевую трубу, причем боковая и задняя поверхности микропористой трубы имеют однородную микропористую структуру и один конец микропористой трубы соединен с впускной кольцевой трубой, а второй ее конец закрыт. Распределитель позволяет регулировать массовый перенос посредством распределения потоков различных сырьевых материалов в разных зонах в системе совместной подачи сырья с большой разностью скоростей реакции сырьевых материалов, что обеспечивает координирование и оптимизацию системы совместной ...

Способ получения спиро[2.4]гепта-4,6-диена

Предложен способ получения спиро[2.4]гепта-4,6-диена, заключающийся в том, что к предварительно нагретой до кипения (40-45°С) смеси 1,2-дихлорэтана с циклопентадиеном прибавляют 50%-ный мас. водный раствор NaOH в присутствии катализатора фазового переноса и процесс ведут при мольном соотношении циклопентадиен : 1,2-дихлорэтан : катализатор : NaOH = 1 : 1 : 0,001-0,01 : 2,5-6 с последующим выделением целевого продукта из реакционной смеси перегонкой с водяным паром. Процесс проводят в одном реакторе и выход целевого продукта составляет 75-90%. Техническим результатом предлагаемого способа является повышение выхода целевого продукта (75-90%), а также упрощение технологии процесса за счет проведения всех стадий в одном реакторе без использования вакуумной дистилляции и органических растворителей, что повышает его экологичность. 2 з.п. ф-лы.

Alkylation of aromatic hydrocarbons by borate esters

The alkylation of an aromatic hydrocarbon is effected with an aliphatic borate in the presence of sulphuric or hydrofluoric acid containing not more than 10% weight of water. The aliphatic groups in the borate may contain 2-25 carbon atoms derived from paraffins, particularly n-paraffins, or cycloparaffins and the borate may be of the formula (RO)3B, (ROBO)3 or (RO)2-BOB(OR)2 or any mixture thereof, the R groups being hydrogen or alkyl with at least one being alkyl. Mixtures obtained by the oxidation of a paraffin in the presence of boric acid or boric oxide may be used. The aromatic hydrocarbon may contain up to 18 carbons and three fused ring, preferably benzene, and is used in a mol. ratio to alkoxy group in the borate of 4-50:1. The amount of acid catalyst may be 5-100 equivalents per equivalent of alkoxy groups in the borate. Reaction is effected for 1/2 -6 hours at 0-100 DEG C. In the examples dodecyl benzene is obtained from benzene and the product of oxidizing dodecane in the presence ...

Azulenes and production thereof

Complexes are formed between an azulene substituted in the 4- and 8-positions and an alkali metal alkyl, aryl, or aralkyl or a complex thereof with a metallo-hydrocarbon compound. The organo-metallic compound used may be any of those referred to in Specification 808,181. In the examples complexes are formed between 4, 8-dimethylazulene and lithium methyl, lithium ethyl, lithium n-propyl, lithium butyl and lithium phenyl, 4, 8-diphenylazulene and lithium butyl and 4-methyl-8-phenylazulene and lithium phenyl, in solution in ether but are not isolated.ALSO:Azulenes substituted in the 4, 6 and 8 positions are obtained by further treating a 4,8-disubstituted azulene by the process of Specification 808,181 which comprises reacting with an alkali metal alkyl, aryl or aralkyl or metallo-hydrocarbon complex thereof to form an addition compound which is either treated with a compound containing an active hydrogen atom, e.g. water or an alcohol, followed by dehydrogenation of the dihydroazulene so ...

Process for the arylation of aromatic compounds

An aryl (carbocyclic or heterocyclic) group is introduced into an aromatic (carbocyclic or heterocyclic) compound by heating the latter with an aromatic compound containing a nuclear-bound sulphonyl halide or sulphonic acid group or a salt of the latter which decomposes under the reaction conditions, in the presence of a catalyst that is a metal, a metal compound, an organic nitrogen compound, a polyhydric phenol, a quinone or a compound containing an aliphatic group of 6 or more carbon atoms. Reaction temperatures of 125-300 DEG C. and catalyst proportions of 0.0001-0.5 gm. mol. per gm. mol. of arylating agent are specified. Metal catalysts specified are copper, platinum, palladium, ruthenium, sodium, potassium, calcium, cobalt, lead, manganese, mercury, silver, titanium and compounds thereof. Organic nitrogen catalysts include amines, amine salts, amides, azo compounds and nitro compounds. Catalytic polyhydric phenols include polyhydroxy-benzenes and naphthalenes, hydroquinone and pyrogallol ...

PROCEDURE FOR THE CONVERSION OF AROMATIC HYDROCARBONS WITH ITQ-13

PROCEDURE FOR THE PRODUCTION OF AN ALKYLATED AROMATIC CONNECTION

CATALYTIC ALKYLATION OF AROMATUS TO ALKYLBENZENE

4,6,8 TRISUBSTITUTED AZULENES AND PROCESS OF PREPARATION

COMPOSITIONS D'OLIGOMERES DE POLYARYLALCANES CONTENANT DES MOTIFS XYLENE ET LEUR PROCEDE DE FABRICATION

L'invention concerne des compositions d'oligomères de polyarylalcanes constituées du mélange d'au moins un oligomère A et d'au moins un oligomère B, caractérisées en ce que l'oligomère A est un mélange d'isomères de formule: dans laquelle R1, R2 et R3 sont identiques ou différents et représentent H ou CH3, n1 et n2 = 0, 1 et 2 avec n1 + n2 ? 3 chacun des isomères A pouvant avoir des substituants R1, R2 et R3 différents, l'oligomère B est un mélange d'isomères de formule: dans laquelle R4, R5, R6, R7, R8, R9, R10, R11 identiques ou différents et représentent H ou CH3, n'1, n"1 et n4 = 0, 1 ou 2, n'2, n"2, n3, n'3 et n5 = 0 ou 1, n'1 + n"1 + n'2 + n"2 + n3 + n'3 + n4 + n5 ? 2, W est un groupe de liaison trivalent choisi dans le groupe constitué par: et et dont les liaisons vers les groupes sont assurées par des atomes de carbone n'appartenant pas au groupement phényle de W, chacun des isomères B pouvant avoir des substituants R4 à R11 différents. Ces compositions ...

COMPOSITIONS D'OLIGOMERES DE POLYARYLALCANES, LEUR PROCEDE DE FABRICATION

L'invention concerne des compositions d'oligomères de polyarylalcanes constituées du mélange de deux oligomères A et B caractérisés en ce que: l'oligomère A est un mélange d'isomères de formule: dans laquelle R est une chaîne hydrocarbonée linéaire ou ramifiée à n atomes de carbone, n est compris entre 2 et 16, R1, R2 et R3 sont identiques ou différents et représentent H ou CH3, n1 et n2 = 0,1 et 2 avec n1 + n2 ? 3,chacun des isomères A pouvant avoir des substituants R, R1, R2 et R3 différents; l'oligomère B est un mélange d'isomères de formule: dans laquelle: R'i et R"i sont identiques ou di.fférents et ont la même significati.on que R; R4, R5, R6, R7, R8, R9, Rlo, Rll sont identiques ou diEférents et représentent H ou CH3, n'l, n 1 et n4 = O, 1 ou 2, n'2, n 2' n3, n'3 et n5 = O ou 1, n'1 + n"1 + n'2 + n"2 + n3 + n'3 + n4 + n5 ? 2, W est un groupe de liaison trivalent choisi dans le groupe constitué par: et et dont les liaisons vers les groupes et sont ...

SYNTHESIS OF LIQUID FUELS AND CHEMICALS FROM OXYGENATED HYDROCARBONS

Processes and reactor systems are provided for the conversion of oxygenated hydrocarbons to hydrocarbons, ketones and alcohols useful as liquid fuels, such as gasoline, jet fuel or diesel fuel, and industrial chemicals. The process involves the conversion of mono-oxygenated hydrocarbons, such as alcohols, ketones, aldehydes, furans, carboxylic acids, diols, triols, and/or other polyols, to C4+ hydrocarbons, alcohols and/or ketones, by condensation. The oxygenated hydrocarbons may originate from any source, but are preferably derived from biomass.

Method for producing sulfonic acid group-containing carbonaceous material, solid acid catalyst, method for producing alkylation reaction product, and method for producing olefin polymer

PRODUCTION Of ALKYLBENZENES

FERRO-SILICATES CRISTALLINS, PROCEDES POUR LES PREPARER ET LEURS APPLICATIONS

L'invention concerne des silicates cristallins. Il s'agit de ferro-silicates cristallins définis d'après leur composition d'ensemble, leur comportement concernant l'adsorption et leur stabilité thermique. Applications : spécialement comme catalyseurs pour l'aromatisation de composés aliphatiques.

Process for producing alkylated aromatic compounds and process for producing phenols

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

Catalyst for producing para-substituted aromatic hydrocarbon and method for producing para-substituted aromatic hydrocarbon using the same

This invention relates to a novel catalyst which enables an efficient production of a high-purity para-substituted aromatic hydrocarbon even without conducting isomerization step and/or adsorption separation step, and more particularly to a catalyst for producing a para-substituted aromatic hydrocarbon, which is formed by coating an MFI-type zeolite having an SiO 2 /Al 2 O 3 ratio (molar ratio) of 20 to 5000 and a primary particle size of not more than 1 μm with a crystalline silicate and is characterized by having a pKa value as measured by a Hammett indicator of not less than −8.

Method and Apparatus for Obtaining Aromatics from Diverse Feedstock

The process relates to the use of any naphtha-range stream containing a portion of C8+ aromatics combined with benzene, toluene, and other non-aromatics in the same boiling range to produce toluene. By feeding the A8+ containing stream to a dealkylation/transalkylation/cracking reactor to increase the concentration of toluene in the stream, a more suitable feedstock for the methylation reaction can be produced. This stream can be obtained from a variety of sources, including the pygas stream from a steam cracker, “cat naphtha” from a fluid catalytic cracker, or the heavier portion of reformate.

Molecular Sieve Composition (EMM-10), Its Method of Making, and Use for Hydrocarbon Conversions

This invention relates to a process for hydrocarbon conversion comprising contacting a hydrocarbon feedstock with a crystalline molecular sieve, in its ammonium exchanged form or in its calcined form, under conversion conditions to form a conversion product, said crystalline molecular sieve comprising unit cells with MWW topology and is characterized by diffraction streaking from the unit cell arrangement in the c direction as evidenced by the arced hk0 patterns of electron diffraction pattern.

Process for alkylation of toluene to form styrene and ethylbenzene

A process is disclosed for making styrene and/or ethylbenzene by reacting toluene with a C 1 source over a catalyst in at least one radial reactor to form a product stream comprising styrene and/or ethylbenzene.

Chain-selective synthesis of fuel components and chemical feedstocks

A method comprising providing a starting composition comprising a polyunsaturated fatty acid, a polyunsaturated fatty ester, a carboxylate salt of a polyunsaturated fatty acid, a polyunsaturated triglyceride, or a mixture thereof; self-metathesizing the starting composition or cross-metathesizing the starting composition with at least one short-chain olefin in the presence of a metathesis catalyst to form self-/cross-metathesis products comprising: cyclohexadiene; at least one olefin; and one or more acid-, ester-, or salt-functionalized alkene; and reacting cyclohexadiene to produce at least one cycloalkane or cycloalkane derivatives. A method for producing cycloalkanes for jet fuel by providing a starting composition comprising at least one selected from the group consisting of algal and polyunsaturated vegetable oils, subjecting the starting composition to metathesis to produce metathesis product comprising at least one olefin, cyclohexadiene, and at least one acid-, ester-, or salt-functionalized alkene, and reacting the at least one olefin and cyclohexadiene to form cycloalkane(s).

PROCESS TO MAKE PROPYLENE FROM ETHYLENE AND EITHER DIMETHYL ETHER, OR METHANOL AND DIMETHYL ETHER

The present invention is a process to make propylene comprising: 1. Process to make propylene comprising:a) providing a reaction zone containing a catalyst;b) introducing a feedstock comprising ethylene, dimethyl ether or a mixture of methanol and dimethyl ether comprising at least 1000 wppm of dimethyl ether, optionally steam into said reaction zone and into contact with said catalyst;c) operating said reaction zone at temperature and pressure conditions to produce an effluent comprising propylene, hydrocarbons, steam, optionally unconverted methanol and/or unconverted dimethyl ether and optionally unconverted ethylene;d) sending the effluent of step c) to a fractionation zone to recover propylene optionally methanol and for dimethyl ether and optionally ethylene;e) optionally recycling at least a part of methanol and/or dimethyl ether and optionally recycling at least a part of ethylene to the reaction zone at step b);wherein the catalyst is an acid and the temperature at the inlet of the reaction zone is under 280° C. and advantageously from 50 to 280° C.2. Process according to wherein the WHSV of the sum of (i) ethylene and of (ii) dimethyl ether or methanol and dimethyl ether is from 0.01 to 100 h-1.3. Process according to wherein MeOH is converted at least partially to DME rich feedstock in a separate dehydration zone and then sent to the reaction zone a).4. Process according to wherein the amount of ethylene being fed to the reaction zone a) is from 0.05 to 20 claim 1 , as determined by the mole ratio of ethylene to the sum of the number of moles of methanol and two times the number of moles of dimethyl ether.5. Process according to wherein the mole ratio of ethylene to the sum of the number of moles of methanol and two times the number of moles of dimethyl ether is at least 0.2.6. Process according to wherein the mole ratio of ethylene to the sum of the number of moles of methanol and two times the number of moles of dimethyl ether is at least 0.3.7. Process ...

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. 1. A method for producing xylenes comprising the steps of:a. loading a zeolite catalyst into a fixed bed reactor system;b. feeding a feedstock to the fixed bed reactors, wherein the feedstock comprises at least one aromatic compound, methanol and water;c. reacting the feedstock in the presence of the zeolite catalyst to form an effluent, wherein the effluent comprises water, aromatic hydrocarbons, and light hydrocarbons;d. cooling the effluent;e. feeding the cooled effluent into a separator;f. separating a vapor phase stream, an aqueous stream, and hydrocarbon stream in the separator;g. distilling the hydrocarbon stream in a distillation section to form a product fraction and a fraction containing unreacted aromatic compounds;h. recycling a portion of the fraction containing unreacted aromatic compounds to the fixed bed reactor system; andi. diverting the vapor phase stream away from the fixed bed reactor system.2. The method of claim 1 , wherein the fixed bed reactor system comprises a single or a plurality of fixed reactors.3. The method of claim 2 , wherein the plurality of reactors is arranged in series.4. The method of claim 2 , wherein the plurality of reactors is arranged in parallel.5. The method of claim 1 , wherein the fixed bed reactor system is operated at a temperature of 420-600° C. and pressure of 10-100 psig.6. The method of claim 1 , wherein the fixed bed reactor system is operated at a temperature of 480-550° C. and pressure of 20-50 psig.7. The method of claim 1 , wherein the WHSV is in the range of 2-12 hr.8. The method of claim 1 , wherein the WHSV is in the range of 4-8 hr.9. The method of claim 1 , wherein the at least one aromatic compound is selected from the group consisting of benzene claim 1 , toluene and a ...

Fluid Bed Reactor with Staged Baffles

The invention relates to a process of alkylating aromatic hydrocarbons, and more particularly a process of making paraxylene by alkylation of benzene and/or toluene with methanol and/or dimethyl ether, and to an apparatus for carrying out said process, the improvement comprising staged injection of one of the reactants, with the stages separated by structured packing so as to minimize at least one of gas phase back-mixing, by-pass phenomena, and gas bubble size.

Supported nano sized zeolite catalyst for alkylation reactions

A catalyst containing nanosize zeolite particles supported on a support material for alkylation reactions, such as the alkylation of benzene to form ethylbenzene, and processes using such a catalyst is disclosed.

Alkylation of Benzene and/or Toluene with Methanol

The present inventors have surprisingly discovered that paraxylene selectivity is found to increase as the amount of coke on catalyst increases. In embodiments the paraxylene selectivity and productivity is maximized by controlling the amount of coke on the catalyst while maintaining xylene yield at an acceptable value. The control of coke may be achieved by one or a combination of the following techniques: increasing catalyst on-oil time, decreasing catalyst residence time in the regenerator, reducing the air or oxygen supply to the regenerator, and decreasing catalyst circulation rate, or a combination thereof. 1. In a process for the alkylation of benzene and/or toluene with methanol in the presence of a catalyst suitable for said alkylation and characterized as a porous crystalline material having a Diffusion Parameter for 2 ,2 dimethylbutane of 0.1-15 secwhen measured at a temperature of 120° C. and a 2 ,2 dimethylbutane pressure of 60 torr (8 kPa) , in an apparatus comprising a fluidized bed reactor and a regenerator , including a cycling of said catalyst between said reactor , wherein coke is deposited on said catalyst by contacting said benzene and/or toluene with methanol in the presence of said catalyst under conversion conditions for a predetermined on-oil cycle time , and said regenerator , wherein coke is removed from said catalyst under regeneration conditions for a predetermined residence time , the improvement comprising carrying out said process so as to maintain coke deposits on said catalyst in the range of greater than 0.5 wt % to no more than 5.0 wt % , based on the weight of said catalyst , and maintaining said contacting under conditions , including on-oil cycle time , catalyst residence time in said regenerator , and catalyst recirculation rate , so as to maintain the coke deposits on said catalyst within said range.2. The process of claim 1 , including regenerating or rejuvenating said catalyst by treatment under oxidative conditions claim 1 ...

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.

Process for the Purification of Paraxylene

The proposed process uses crystallization technology to purify paraxylene simultaneously of large concentrations of C8 aromatics and also small concentrations of oxygenated species. 110.-. (canceled)11. A process comprising selective production of paraxylene by the alkylation of benzene and/or toluene including a step of oxygenate removal and then a step of removal of high concentrations of C8 aromatics by simulated counter-current adsorption.12. The process of claim 11 , wherein said alkylation comprises the contact of benzene and/or toluene with an alkylating agent in the presence of a catalyst comprising a porous crystalline material having a Diffusion Parameter for 2 claim 11 ,2 dimethylbutane of about 0.1-15 secwhen measured at a temperature of 120° C. and a 2 claim 11 ,2 dimethylbutane pressure of 60 torr (8 kPa) wherein said porous crystalline material has undergone prior treatment with steam at a temperature of at least 950° C. to adjust the Diffusion Parameter of said material to about 0.1-15 sec.13. The process of claim 12 , wherein said Diffusion Parameter of said porous crystalline material is about 0.5-10 sec.14. The process of claim 12 , wherein said porous crystalline material has undergone prior treatment with steam at a temperature of at least 1000° C. for between about 10 minutes and about 100 hours.15. The process of claim 14 , wherein said treatment with steam reduces the pore volume of the catalyst to not less than 50% of that of the pore volume of the catalyst before said treatment with steam.16. The process of claim 12 , wherein the catalyst contains at least one oxide modifier selected from the group consisting of oxides of elements of Groups IIA claim 12 , IIIA claim 12 , IIIB claim 12 , IVA claim 12 , IVB claim 12 , VA and VIA of the Periodic Table.17. The process of claim 12 , wherein the catalyst contains at least one oxide modifier selected from the group consisting of oxides of boron claim 12 , magnesium claim 12 , calcium claim 12 , ...

METHODS OF PRODUCING PARA-XYLENE AND TEREPHTHALIC ACID

The present disclosure provides methods to produce para-xylene, toluene, and other compounds from renewable sources (e.g., cellulose, hemicellulose, starch, sugar) and ethylene in the presence of a catalyst. For example, cellulose and/or hemicellulose may be converted into 2,5-dimethylfuran (DMF), which may be converted into para-xylene by cycloaddition of ethylene to DMF. Para-xylene can then be oxidized to form terephthalic acid. 1. A method for producing para-xylene , comprising:a) providing 2,5-hexanedione;b) providing ethylene;c) providing a catalyst;d) combining the 2,5-hexanedione, the ethylene, and the catalyst to form a reaction mixture; ande) producing para-xylene from at least a portion of the 2,5-hexanedione in the reaction mixture.2. The method of claim 1 , further comprising isolating para-xylene from the reaction mixture.3. The method of claim 1 , further comprising providing a solvent system claim 1 , and combining the 2 claim 1 ,5-hexanedione claim 1 , the ethylene claim 1 , the catalyst claim 1 , and the solvent system to form the reaction mixture.4. The method of claim 3 , wherein the solvent system comprises an aprotic solvent.5. The method of claim 3 , wherein the solvent system comprises an ether solvent.6. The method of claim 3 , wherein the solvent system comprises a C1-C20 aliphatic solvent claim 3 , a C6-C20 aromatic solvent claim 3 , an alkyl phenyl solvent claim 3 , a C2-C20 ether claim 3 , a C2-C20 ester claim 3 , a C1-C20 alcohol claim 3 , a C2-C20 ketone claim 3 , or any combinations or mixtures thereof.7. The method of claim 3 , wherein the solvent system comprises dimethylacetamide claim 3 , acetonitrile claim 3 , sulfolane claim 3 , dioxane claim 3 , dioxane claim 3 , dimethyl ether claim 3 , diethyl ether claim 3 , glycol dimethyl ether (monoglyme) claim 3 , ethylene glycol diethyl ether (ethyl glyme) claim 3 , diethylene glycol dimethyl ether (diglyme) claim 3 , diethylene glycol diethyl ether (ethyl digylme) claim 3 , triethylene ...

Alkylation Process

The invention relates to the production of paraxylene by an alkylation process that also produces oxygenates. The process is controlled to utilize recycle to minimize said oxygenates. 1. A process for the production of paraxylene by alkylation of aromatic hydrocarbons with methanol in the presence of at least one molecular sieve comprising:(a) providing a feed comprising an alkylating agent selected from methanol, dimethylether, and mixtures thereof, and an aromatic hydrocarbon selected from benzene, toluene, and mixtures thereof, to a reactor;(b) contacting in said reactor said alkylating agent and aromatic hydrocarbon in the presence of at least one molecular sieve and under conditions suitable for the production of paraxylene selectively;(c) obtaining a stream comprising (i) paraxylene, (ii) unreacted alkylating agent, (iii) unreacted aromatic hydrocarbon, (iv) water, and at least one oxygenate (other than water and said alkylating agent(s)) co-produced with paraxylene in step (a);(d) separating (i), (ii), (iii), and (iv) into plural streams, each containing said at least one oxygenate; and(e) recycling at least one of said plural streams comprising at least one of (ii), (iii), and (iv) to step (a) without a step of separation of said at least one oxygenate from said at least one plural streams.2. The process of claim 1 , including a step of determining the concentration of at least one of an oxygenate other than methanol and/or dimethylether produced in said reactor and/or determining the concentration of at least one of an oxygenate other than methanol and/or dimethylether provided to said reactor at a first preselected time and comparing at least one of said concentrations with a predetermined concentration or at least one of said concentrations determined at a second predetermined time claim 1 , different from said first predetermined time.3. The process of claim 1 , including a step of attenuating at least one process parameter so that the output of at least ...

PHOSPHORUS MODIFIED ZEOLITE CATALYSTS

An unbound catalyst composition comprises a zeolite and phosphorus in an amount between about 0.01 wt % and about 3 wt % of the total catalyst composition. The catalyst composition, as calcined at ˜1000° F. (˜538° C.) for at least ˜3 hours, can exhibit (i) 2,2-dimethylbutane diffusivity >1.5×10secwhen measured at ˜120° C. and ˜60 torr (˜8 kPa), (ii) coke deactivation rate constant <˜0.15, and (iii) alpha value at least 10, and further exhibiting at least one of: (a) mesoporosity >0.2 ml/g; (b) microporous surface area at least 375 m/g; and (c) coke deactivation rate constant <0.05 after steaming in ˜100% steam for ˜96 hours at ˜1000° F. (˜538° C.). 2. The catalyst composition of claim 1 , wherein the alpha value is at least 20.3. The catalyst composition of claim 1 , wherein the alpha value is at least 50.4. The catalyst composition of claim 1 , wherein the mesoporosity is greater than 0.3 ml/g.5. The catalyst composition of claim 1 , wherein the microporous surface area is at least 380 m/g.6. The catalyst composition of claim 1 , wherein the 2 claim 1 ,2-dimethylbutane diffusivity is at least 1.7×10sec claim 1 , when measured at a temperature of about 120° C. and a 2 claim 1 ,2-dimethylbutane pressure of about 60 torr (about 8 kPa).7. The catalyst composition of claim 1 , wherein the 2 claim 1 ,2-dimethylbutane diffusivity is at least 2×10sec claim 1 , when measured at a temperature of about 120° C. and a 2 claim 1 ,2-dimethylbutane pressure of about 60 torr (about 8 kPa).8. The catalyst composition of claim 1 , wherein the coke deactivation rate constant is less than or equal to 0.04 after steaming in approximately 100% steam for about 96 hours at about 1000° F. (about 538° C.).9. The catalyst composition of claim 1 , wherein the composition has at least two of said properties (a) to (c).10. The catalyst composition of claim 1 , wherein said zeolite has a constraint index from about 1 to about 12.11. The catalyst composition of claim 1 , wherein said zeolite ...

Hydrocarbon Conversion Process

The invention relates to processes for converting a mixture of hydrocarbon and oxygenate into products containing acetylene and carbon monoxide. The invention also relates to utilizing at least a portion of the acetylene and carbon monoxide for producing xylenes such as p-xylene, utilizing at least a portion of xylenes for producing polymeric fibers, and to equipment useful for these processes. 1. A hydrocarbon conversion process , comprising:(a) providing a first mixture, the first mixture comprising ≧10.0 wt. % hydrocarbon and ≧1.0 wt. % oxygenate, the weight percents being based on the weight of the first mixture;(b) exposing the first mixture a temperature ≧700° C. in a first region under pyrolysis conditions to produce a second mixture, the second mixture comprising molecular hydrogen, carbon monoxide, and ≧1.0 wt. % of acetylene based on the weight of the second mixture, wherein the second mixture has a molecular hydrogen:carbon monoxide molar ratio ≧2.0 and a carbon monoxide:acetylene molar ratio ≧0.1;(c) converting at least a portion of the second mixture's acetylene to produce a first intermediate mixture comprising ≧10.0 wt. % aromatic hydrocarbon based on the weight of the intermediate mixture;(d) reacting at least a portion of the second mixture's carbon monoxide with at least a portion of the second mixture's molecular hydrogen to produce a second intermediate mixture comprising ≧10.0 wt. % alcohol based on the weight of the second intermediate mixture; and(e) reacting at least a portion of the first intermediate mixture's aromatics with at least a portion of the second intermediate mixture's alcohol to produce a product comprising water and ≧10.0 wt. % p-xylene based on the weight of the product.2. The process of claim 1 , wherein the first mixture comprises ≧25.0 wt. % of hydrocarbon and ≧10.0 wt. % of oxygenate claim 1 , the oxygenate having an Effectiveness Factor ≧0.05 claim 1 , and further comprises ≧5.0 wt. % molecular hydrogen claim 1 , the ...

Process for the Production of Xylenes and Light Olefins

In a hydrocarbon upgrading process, a hydrocarbon feed is treated in at least one of a steam cracker, catalytic cracker, coker, hydrocracker, and reformer under suitable conditions to produce a first stream comprising olefinic and aromatic hydrocarbons. A second stream composed mainly of Cto Colefinic and aromatic hydrocarbons is recovered from the first stream and at least part of the second stream is contacted with a catalyst in the absence of added hydrogen under reaction conditions including a temperature of about 450° C. to about 70° C. effective to dealkylate, transalkylate, crack and aromatize components of the second stream to produce a third stream having an increased benzene and/or toluene content compared with the second stream and a C− olefin by-product. The C− olefin by-product and a fourth stream comprising toluene are then recovered from the third stream. 1. A hydrocarbon upgrading process comprising:(a) treating a hydrocarbon feed in at least one of a steam cracker, catalytic cracker, coker, hydrocracker, and reformer under suitable conditions to produce a first stream comprising olefinic and aromatic hydrocarbons;{'sub': 4', '12, '(b) recovering from said first stream a second stream composed mainly of Cto Colefinic and aromatic hydrocarbons;'}{'sub': '3', '(c) contacting at least part of the second stream with a catalyst in the absence of added hydrogen under reaction conditions including a temperature of about 450° C. to about 700° C. effective to dealkylate, transalkylate, crack and aromatize components of said second stream to produce a third stream having an increased benzene and/or toluene content compared with said second stream and a C− olefin by-product;'}{'sub': '3', '(d) recovering C− olefins from said third stream; and'}(e) separating a fourth stream comprising toluene from said third stream.2. The process of claim 1 , wherein the first hydrocarbon stream is selected from natural gas liquids claim 1 , natural gas condensate claim 1 , ...

Process for the Production of Xylenes and Light Olefins

In a hydrocarbon upgrading process, a hydrocarbon feed is treated in at least one of a steam cracker, catalytic cracker, coker, hydrocracker, and reformer under suitable conditions to produce a first stream comprising olefinic and aromatic hydrocarbons. A second stream composed mainly of C 4 + olefinic and aromatic hydrocarbons is recovered from the first stream and is fed together with a methylating agent to a reaction zone containing a catalyst under reaction conditions including a temperature of about 450° C. to about 700° C., such that aromatics components in the second stream undergo dealkylation, transalkylation and/or methylation and aliphatic components undergo cracking and aromatization to produce a third stream having an increased xylene content compared with said second stream and a C 3 − olefin by-product. The C 3 − olefin by-product is recovered and para-xylene is removed from at least part of said third stream.

Process for the Production of Xylenes and Light Olefins

In a hydrocarbon upgrading process, a hydrocarbon feed is treated in at least one of a steam cracker, catalytic cracker, coker, hydrocracker, and reformer under suitable conditions to produce a first stream comprising olefinic and aromatic hydrocarbons. A second stream composed mainly of C 4 to C 12 + olefinic and aromatic hydrocarbons is recovered from the first stream and blended said second stream with a residual fraction from a steam cracker or an atmospheric or vacuum distillation unit to produce a third stream. The third stream is then catalytically pyrolyzed in a reactor under conditions effective to produce a fourth stream having an increased benzene and/or toluene content compared with said second stream and a C 3 -olefin by-product. The C 3 -olefin by-product is recovered and benzene and/or toluene are recovered from the fourth stream.

Hydrocarbon Conversion Process

The invention relates to methods and equipment for converting C olefin to, e.g., one or more of di-C olefin, oligomers and polymers of C olefin, branched C-aldehydes, C-carboxylic acids, and C oxygenates. The invention encompasses producing methyl tert-butyl ether and diisobutylene, and converting methyl tert-butyl ether to isobutylene. 1. An olefin upgrading method comprising:{'sub': '3+', '(a) providing a first olefin mixture and a first process fluid, the first olefin mixture comprising ≧0.1 wt. % of C olefins based on the weight of the first olefin mixture, and the first process fluid comprising ≧10.0 wt. % alcohol based on the weight of the first process fluid;'}{'sub': 3+', '3+, '(b) reacting the first olefin mixture and the first process fluid to produce a first reaction mixture, the first reaction mixture comprising ether and di-C olefin and having a di-C olefin:ether molar ratio≧1.0;'}{'sub': 3+', '3+', '3+, "(c) separating from the first reaction mixture a second olefin mixture and a first product, wherein (A) the second olefin mixture comprises ≧0.1 wt. % of C olefins based on the weight of the second olefin mixture and (B) the first product (i) comprises at least a portion of the first reaction mixture's di-C olefin and at least a portion of the first reaction product's ether and (ii) has a di-C olefin:ether molar ratio≧1.0;"}{'sub': '3+', '(d) providing a third olefin mixture and a second process fluid, the third olefin mixture comprising ≧1.0 wt. % of C olefin based on the weight of the third olefin mixture, the third olefin mixture containing at least a portion of the second olefin mixture, and the second process fluid comprising ≧10.0 wt. % alcohol based on the weight of the second process fluid; and'}{'sub': '3+', '(e) reacting the third olefin mixture and the second process fluid to produce a second reaction mixture, the second reaction mixture comprising ether and having di-C olefin:ether molar ratio<1.0.'}2. The method of claim 1 , wherein (i) ...

PROCESS AND PLANT FOR THE PRODUCTION OF LOW-MOLECULAR OLEFINS

In the production of low-molecular olefins, in particular of ethylene and propylene, an educt stream (O) containing at least one oxygenate and an educt stream (C) containing at least one C olefin are simultaneously converted in at least one identical reactor on an identical catalyst to obtain a product mixture (P) comprising low-molecular olefins and gasoline hydrocarbons. The ratio (V) of oxygenates in the educt stream (O) to C olefins in the educt stream (C) here is 0.05 to 0.5 and is calculated according to the following formula: 2. The process according to claim 1 , wherein in a first separating means the product mixture (P) is separated into a mixture (H) rich in C olefins and a stream (B) containing C olefins claim 1 , that in a second separating means the stream (B) containing C olefins is separated into a stream (F) substantially containing Cfractions claim 1 , a stream (A) rich in C gasoline hydrocarbons claim 1 , and a recyling stream (R) and that the recycling stream (R) is at least partly recirculated to the at least one reactor claim 1 , wherein the molar ratio between the recycling stream (R) and the educt stream (C) containing C olefins lies between 0.1 and 1.5.3. The process according to claim 2 , wherein the second separating means is operated at a pressure of 4-15 bar claim 2 , and the recycling stream (R) is withdrawn as side draw claim 2 , and recirculated directly into a conduit opening into the reactor.4. The process according to claim 1 , wherein the educt stream (O) containing oxygenates is divided into several partial streams and each partial stream is passed onto one of at least two catalyst beds in the reactor.5. The process according to claim 1 , wherein as catalyst a form-selective zeolite material is used.6. The process according to claim 1 , wherein the educt stream (O) containing oxygenates contains at least one alcohol.7. The process according to claim 1 , wherein the pressure at the inlet of the reactor lies between 1.5 and 10 bar.8 ...

Recovery of Olefins from Para-Xylene Process

A process for producing para-xylene, by (a) contacting toluene with methanol in the presence of an alkylation catalyst under conditions effective to produce an alkylation effluent comprising xylenes and a by-product mixture comprising water, dimethyl ether and C− hydrocarbons; (b) separating the alkylation effluent into a first fraction containing xylenes and a second fraction containing the by-product mixture; (c) removing water from the second fraction to produce a dried by-product mixture; (d) fractionating the dried by-product mixture to separate the mixture into a bottoms stream containing dimethyl ether and an overhead stream containing at least some of the C- hydrocarbons; and (e) recovering ethylene and propylene from the overhead stream. 1. A process for producing para-xylene , the process comprising:{'sub': '4', '(a) contacting toluene and/or benzene with methanol in the presence of an alkylation catalyst under conditions effective to produce an alkylation effluent comprising xylenes and a by-product mixture comprising water, dimethyl ether and C− hydrocarbons;'}(b) separating the alkylation effluent into a first fraction containing xylenes and a second fraction containing the by-product mixture;(c) removing water from the second fraction to produce a dried by-product mixture;{'sub': '4', '(d) fractionating the dried by-product mixture to separate the mixture into a bottoms stream containing dimethyl ether and an overhead stream containing at least some of the C− hydrocarbons; and'}(e) recovering ethylene and propylene from the overhead stream.2. The process of claim 1 , wherein water is removed from said second fraction by passing the second fraction through a molecular sieve drier.3. The process of claim 1 , wherein water is removed from said second fraction by washing the second fraction with methanol.4. The process of claim 3 , further comprising passing the methanol through a molecular sieve drier prior to washing the second fraction with the methanol ...

METHOD OF ALKYLATING OR ACYLATING AN ARENE

A method of alkylating or acylating an arene includes reacting the arene with an organic halide in the presence of an aprotic solvent and a catalyst of formula (I) 1. A method of alkylating or acylating an arene , the method comprising: {'br': None, 'sup': 1', '2', '3, 'sub': m', 'n, 'MRX.Z(R)(R)\u2003\u2003(I)'}, 'reacting an arene with an organic halide selected from the group consisting of unsubstituted or substituted tertiary alkyl halides, unsubstituted or substituted allyl halides, unsubstituted or substituted benzyl halides, and unsubstituted or substituted acyl halides in the presence of a catalyst and an aprotic solvent; wherein the catalyst is of formula (I)'}whereinM is Al, Ga, or Fe;{'sup': '1', 'sub': 1', '12, 'Ris C-Calkyl;'}m is 0 or 1;{'sup': 2', '3, 'sub': 2', '12, 'Rand Rare each independently unsubstituted or substituted C-Calkyl;'}each occurrence of X is independently a halogen;n is 2 or 3;the sum of m and n is 3; andZ is S or O;{'sup': 2', '3, 'provided that when M is Al, then m is 1, n is 2, and Rand Rare each independently substituted with at least one electron-withdrawing group; and'}provided that when M is Ga or Fe, then m is 0 and n is 3.2. The method of claim 1 , wherein the arene is an unsubstituted or substituted C-Carene.3. The method of claim 1 , wherein the arene is an unsubstituted or substituted benzene.4. The method of claim 1 , wherein the arene is a monosubstituted benzene.5. The method of claim 1 , wherein the organic halide is selected from the group consisting of C-Ctertiary alkyl chlorides claim 1 , allyl chloride claim 1 , benzyl chloride claim 1 , and C-Cacyl chlorides.6. The method of claim 1 , wherein the organic halide is t-butyl chloride or acetyl chloride.7. The method of claim 1 , wherein the aprotic solvent is an aliphatic aprotic solvent.8. The method of claim 1 , wherein the aprotic solvent is a C-Calkane.9. The method of claim 1 , wherein M is Al claim 1 , Ris ethyl claim 1 , and each occurrence of X is chloro.10. ...

Processes and apparatuses for toluene and benzene methylation in an aromatics complex

This present disclosure relates to processes and apparatuses for toluene and benzene methylation in an aromatics complex for producing paraxylene. More specifically, the present disclosure relates to processes and apparatuses for toluene and benzene methylation within an aromatics complex for producing paraxylene wherein an embodiment uses a reactor having a refractory comprising a low iron content refractory.

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 ...

USE OF METAL-ACCUMULATING PLANTS FOR THE PREPARATION OF CATALYSTS THAT CAN BE USED IN CHEMICAL REACTIONS

A method of implementing organic synthesis reactions uses a composition containing a metal catalyst originating from a calcined plant. The plants can be from the Brassicaceae, Sapotaceae and Convolvulaceae family, and the metal catalyst contains metal in the M(II) form such as zinc, nickel, manganese, lead, cadmium, calcium, magnesium or copper. Examples of the organic synthesis reactions include halogenations, electrophilic reactions, cycloadditions, transesterification reactions and coupling reactions, among others. 1. A method for the implementation of an organic synthesis reaction , comprising: [{'sup': 2+', '2+', '3+', '+', '+, 'wherein said at least one metal in the M(II) form is selected from the group consisting of zinc (Zn), nickel (Ni), and manganese (Mn), said metal in the M(II) form having been accumulated by the plant during its growth in a soil containing said metal and at least one cationic species selected from the group consisting of MgCa, Fe, Na and K which have not been accumulated by said plant but are physiologically present in said plant and originate from the latter; and'}, 'bringing the composition into contact with at least one chemical compound capable of reacting with said composition., 'providing a composition comprising at least one metal catalyst containing a metal in the M(II) form, said metal originating from a calcined plant or calcined plant part, said composition having been acid treated,'}2. The method according to claim 1 , wherein the organic synthesis reaction is selected from halogenations claim 1 , electrophilic aromatic reactions in series claim 1 , synthesis of 3 claim 1 ,4-dihydropyrimidin-2(1H)-one or 3 claim 1 ,4-dihydropyrimidin-2(1H)-thione claim 1 , cycloaddition reactions claim 1 , transesterification reactions claim 1 , catalyst synthesis reactions for coupling or hydrogenation reactions after reduction of Ni(II) to Ni(0) claim 1 , synthesis of amino acid or oxime developers claim 1 , and hydrolysis of sulphur- ...

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.

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 ...

Method for Providing a Co-Feed in the Coupling of Toluene with a Carbon Source

A process for making styrene is disclosed that includes reacting toluene with a C 1 source and a co-feed in the presence of a catalyst in a reactor to form a first product stream comprising styrene, ethylbenzene, carbon monoxide, and hydrogen; separating the hydrogen and carbon monoxide from the first product stream to form a second stream; separating the hydrogen from the second stream to form a third stream comprising hydrogen and a fourth stream comprising carbon monoxide; wherein the fourth stream is recycled to the reactor and forms at least a portion of the co-feed.

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 ...

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

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

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.

METHOD FOR PRODUCING ALKYL SUBSTITUTED BENZENE

A method for producing alkyl substituted benzene includes (a) providing a starting material selecting from the group consisting of furan, an alkyl substituted furan, 2-methylfuran, 2,3-dimethylfuran, 2,4-dimethylfuran, 2,5-dimethylfuran, 2,5-hexanedione, and combinations thereof, and (b) subjecting the starting material to a cycloaddition reaction with a monoene in the absence of solvent and in the presence of the metal triflate catalyst to produce an alkyl substituted benzene. 1. A method for producing alkyl substituted benzene , comprising the steps of:(a) providing a starting material selecting from the group consisting of furan, an alkyl substituted furan, 2-methylfuran, 2,3-dimethylfuran, 2,4-dimethylfuran, 2,5-dimethylfuran, 2,5-hexanedione, and combinations thereof; and(b) subjecting the starting material to a cycloaddition reaction with a monoene in the absence of solvent and in the presence of the metal triflate catalyst to produce an alkyl substituted benzene.2. The method according to claim 1 , wherein the metal trilflate catalyst is selected from the group consisting of copper (II) trifluoromethanesulfonate claim 1 , zinc trifluoromethanesulfonate claim 1 , scandium trifluoromethanesulfonate claim 1 , yttrium trifluoromethanesulfonate claim 1 , yttrium trifluoromethanesulfonate hydrate claim 1 , indium(III) trifluoromethanesulfonate claim 1 , and combinations thereof.3. The method according to claim 2 , wherein claim 2 , instep (d) claim 2 , a molar ratio of the metal triflate catalylst to the starting material ranging from 1:50 to 1:100000.4. The method according to claim 3 , wherein claim 3 , instep (d) claim 3 , a molar ratio of the metal triflate catalylst to the starting material ranging from 1:5000 to 1:30000.5. The method according to claim 1 , wherein the monoene is selected from the group consisting of ethylene claim 1 , propene claim 1 , 1-hexene claim 1 , cyclohexene claim 1 , and combinations thereof.6. The method according to claim 1 , ...

PHOSPHINE SUBSTITUTED FERROCENYL COMPLEX

A functionalized magnetic nanoparticle including an organometallic sandwich compound and a magnetic metal oxide. The functionalized magnetic nanoparticle may be reacted with a metal precursor to fol in a catalyst for various C—C bond forming reactions. The catalyst may be recovered with ease by attracting the catalyst with a magnet. 2. (canceled)3. The complex of claim 1 , wherein Ris an optionally substituted alkyl.4. The complex of claim 1 , wherein Ris an optionally substituted aryl.5. The complex of claim 1 , wherein X is NH.620-. (canceled) This application claims the priority of the filing date of the U.S. Provisional Patent Application No. 62/406,449 filed Oct. 11, 2016, the disclosure of which is hereby incorporated herein by reference in its entirety.This project was funded by the National Plan for Science, Technology and Innovation (MAARIFAH)-King Abdulaziz City for Science and Technology through the Science and Technology Unit at King Fahd University of Petroleum and Minerals (KFUPM), the Kingdom of Saudi Arabia, award number 15-NAN4650-04.Aspects of this technology are described in an article “Magnetic nanoparticle-supported ferrocenylphosphine: a reusable catalyst for hydroformylation of alkene and Mizoroki-Heck olefination” by M. Nasiruzzaman Shaikh, Md. Abdul Aziz, Aasif Helal, Mohamed Bououdina, Zain H. Yamania, and Tae-Jeong Kim, in RSC Advances, 2016, pages 41687-41695, which is incorporated herein by reference in its entirety.The present disclosure relates to a functionalized magnetic nanoparticle including an organometallic sandwich compound and a functional group which can bind to a nanoparticle. The disclosure also relates to a magnetic catalyst which catalyzes C—C bond forming reactions such as hydroformylation and the Mizoroki-Heck coupling reaction.Carbon-carbon bond formation reactions mediated by various transition metals have emerged as increasingly important methodologies for the preparation of numerous organic building blocks for drugs, ...

Fullerene Derivatives and Their Applications in Organic Photovoltaics

The present invention relates to new fullerene derivatives of formulae 1a-d, 2 and 3: method of synthesizing said derivatives, and applications thereof in organic photovoltaics, e.g., organic solar cells. In particular, the fullerene derivatives of the present invention are soluble in non-halogenated solvents such that an environmental-friendly and low-cost fabrication method for industrialization of solar cell based on the new fullerene derivatives is provided. An ink formulation for forming a thin film on a substrate of organic photovoltaics comprising at least one of the fullerene derivatives of the present invention is also provided. Greater than 3% power conversion efficiency of the organic solar cells (area=0.16 cm 2 ) formed based on the fullerene derivatives of the present invention with less pollution and lower cost in fabrication can be achieved in the present invention.

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.

Methods of Refining Natural Oil Feedstocks

Methods are provided for refining natural oil feedstocks. The methods comprise reacting the feedstock in the presence of a metathesis catalyst under conditions sufficient to form a metathesized product comprising olefins and esters. In certain embodiments, the methods further comprise separating the olefins from the esters in the metathesized product. In certain embodiments, the methods further comprise hydrogenating the olefins under conditions sufficient to form a fuel composition. In certain embodiments, the methods further comprise transesterifying the esters in the presence of an alcohol to form a transesterified product. 119-. (canceled)20. A method of producing a fuel composition comprising:providing a feedstock comprising natural oil glycerides, and (b) low-molecular-weight olefins;reacting the natural oil glycerides with the low-molecular-weight olefins in the presence of a metathesis catalyst to form a metathesized product comprising olefins and esters;separating at least a portion of the olefins in the metathesized product from the esters in the metathesized product; andhydrogenating the separated olefins to form a fuel composition.21. The method of claim 20 , wherein the fuel composition is: (a) a kerosene-type jet fuel having a carbon number distribution between 8 and 16 claim 20 , a flash point between 38° C. and 66° C. claim 20 , an auto ignition temperature of 210° C. claim 20 , and a freeze point between −47° C. and −40° C.; (b) a naphtha-type jet fuel having a carbon number distribution between 5 and 15 claim 20 , a flash point between −23° C. and 0° C. claim 20 , an auto ignition temperature of 250° C.; and a freeze point of −65° C.; or (c) a diesel fuel having a carbon number distribution between 8 and 25 claim 20 , a specific gravity of between 0.82 and 1.08 at 15.6° C. claim 20 , a cetane number of greater than 40; and a distillation range between 180° C. and 340° C.22. The method of claim 20 , further comprising flash-separating a light end ...

Treatment of Off-Gas in the Production of Para-Xylene by the Methylation of Toluene and/or Benzene

A process for removing contaminants from an off-gas stream generated by the methylation of toluene and/or benzene by methanol to produce para-xylene. The treated off-gas stream, which contains C hydrocarbons, may be further processed in an olefins plant/process to yield valuable light alkanes and olefins. 1. A process for producing para-xylene , the process comprising:{'sub': '4', '(a) contacting toluene and/or benzene with methanol in the presence of an alkylation catalyst under conditions effective to produce an alkylation effluent comprising xylenes and a by-product mixture comprising water, dimethyl ether, C− hydrocarbons, and contaminants;'}(b) separating the alkylation effluent into a first fraction containing xylenes and a second fraction containing the by-product mixture;(c) recovering para-xylene from the first fraction; and(d) treating the second fraction to remove the contaminants.2. The process of claim 1 , wherein the para-xylene is recovered by fractional crystallization or selective adsorption.3. The process of claim 1 , wherein the treating (d) is accomplished by counter-currently contacting the second fraction with a C-Chydrocarbon absorbent in an absorber demethanizer.4. The process of claim 3 , wherein the absorbent consists essentially of a Cor Chydrocarbon or a mixture thereof.5. The process of claim 3 , wherein the absorbent consists essentially of a Chydrocarbon or a mixture thereof.6. The process of claim 3 , wherein the treating (d) produces an overhead stream comprising hydrogen claim 3 , methane and contaminants and a bottoms stream comprising C hydrocarbons and absorbent claim 3 , and further comprising:{'sub': '2+', '(e) separating the absorbent from the differing C hydrocarbons.'}7. The process of claim 6 , wherein the absorbent recovered in the separating (e) is recirculated to the treating (d).8. The process of claim 6 , wherein the separating (e) is accomplished by a single fractionation column.9. The process of claim 1 , further ...

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- ...

PROCESS FOR THE CYCLOPROPANATION OF OLEFINS USING N-METHYL-N-NITROSO COMPOUNDS

A process of converting a carbon-carbon double bond on a substrate into a cyclopropane ring, which method comprises the step of treating the substrate with a N-alkyl-N-nitroso compound, a transition metal catalyst and an aqueous base, wherein the N-alkyl-N-nitroso compound is formed by reacting an alkyl amine with an alkali metal nitrite in the presence of a mono-basic or di-basic acid, or a mixture thereof, and wherein the N-alkyl-N-nitroso compound is not distilled before it is mixed with the substrate, catalyst and base. 1. A process of converting a carbon-carbon double bond on a substrate into a cyclopropane ring , the process comprising treating the substrate with a N-alkyl-N-nitroso compound , a transition metal catalyst and an aqueous base , wherein the N-alkyl-N-nitroso compound is formed by reacting an alkyl amine with an alkali metal nitrite in the presence of a mono-basic or di-basic acid comprising a mono-basic or di-basic carboxylic acid , or a mixture thereof , and wherein the N-alkyl-N-nitroso compound is not distilled before it is mixed with the substrate , catalyst and base.2. (canceled)3. The process of claim 1 , wherein the acid is formic acid or acetic acid.4. The process according to claim 1 , wherein the acid is a mixture of a mono-basic or di-basic carboxylic acid and an organic or inorganic acid having a lower pKa than said carboxylic acid.5. The process according to claim 4 , wherein the acid is a mixture of acetic acid and sulphuric acid.6. The process according to claim 1 , wherein the N-alkyl-N-nitroso compound is (N-methyl-N-nitroso)-4-amino-4-methyl-2-pentanone.8. The process according to wherein the substrate is an isoprenoid.11. The process according to claim 8 , wherein the isoprenoid is alpha famesene or beta farnesene. This disclosure relates to a method of cyclopropanating alkenes.The conversion of a carbon-carbon double bond to a cyclopropane ring is a chemical transformation used commonly in the synthesis of organic chemical ...

IONIC LIQUID COMPOUND

The present disclosure provides an ionic liquid compound of Formula (I) and its application in reactions such as alkylation, arylation, acylation, diels alder and oligomerization, 2. The ionic liquid compound as claimed in claim 1 , wherein the alkyl group is selected from the group consisting of methyl claim 1 , ethyl claim 1 , propyl claim 1 , butyl and combinations thereof; the aryl group is selected from the group consisting of benzyl claim 1 , phenyl claim 1 , substituted benzenes and combinations thereof; and the halogen is selected from the group consisting of F claim 1 , Cl claim 1 , Br and I.3. The ionic liquid compound as claimed in claim 1 , wherein NRRRis a trialkylamine; Mor Mis a metal selected from the group consisting of Al claim 1 , Fe claim 1 , Zn claim 1 , Mn claim 1 , Mg claim 1 , Ti claim 1 , Sn claim 1 , Pd claim 1 , Pt claim 1 , Rh claim 1 , Cu claim 1 , Cr claim 1 , Co claim 1 , Ce claim 1 , Ni claim 1 , Ga claim 1 , In claim 1 , Sb claim 1 , Zr and combinations thereof; and X or Y is a halogen.5. The process as claimed in claim 4 , wherein the step (i) and/or the step (ii) are carried out at a temperature ranging from −20 to 100° C.6. The process as claimed in claim 4 , wherein the step (i) is carried out in the presence of a solvent selected from the group consisting of ethyl acetate claim 4 , ethanol claim 4 , methanol claim 4 , methyl iso butyl ketone claim 4 , methyl ethyl ketone claim 4 , benzene claim 4 , toluene claim 4 , dichloromethane and combinations thereof and the step (ii) is carried out in the presence of a solvent selected from the group claim 4 , consisting of benzene claim 4 , toluene claim 4 , dichloromethane claim 4 , methyl iso butyl ketone claim 4 , methyl ethyl ketone and combinations thereof.78-. (canceled)9. The process as claimed in claim 4 , wherein the mole ratio of the amine to the metal salt ranges from 1:0.1 to 1:0.5 and the mole ratio of the ionic salt complex precursor to the metal salt ranges from 1:3 and 1: ...

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 ...

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 ...

MAGNETIC PARTICLE-IONIC LIQUID COMPOSITE MATERIALS AND METHODS OF MAKING AND USE THEREOF

Described herein are magnetic particle-ionic liquid composite materials, and methods of making and use thereof. The magnetic particle-ionic liquid composite materials can comprise an ionic liquid conjugated to a magnetic particle, wherein the ionic liquid comprises at least one cation and at least one metal halide anion; and wherein the ionic liquid is not covalently bound to the magnetic particle. 1. A magnetic particle-ionic liquid composite material , comprising:an ionic liquid conjugated to a magnetic particle;wherein the ionic liquid comprises at least one cation and at least one metal halide anion, wherein the ionic liquid is a salt of the at least one cation and the at least one metal halide anion with a melting point of 150° C. or less; andwherein the ionic liquid is not covalently bound to the magnetic particle.2. The composite material of claim 1 , wherein the at least one cation is an ammonium cation claim 1 , an imidazolium cation claim 1 , a pyridinium cation claim 1 , a phosphonium cation claim 1 , a sulphonium cation claim 1 , or a combination thereof.3. The composite material of claim 1 , wherein the at least one cation comprises an ammonium cation of the structure NRRRR claim 1 , wherein R claim 1 , R claim 1 , R claim 1 , and Rare independently H claim 1 , halogen claim 1 , substituted or unsubstituted C-Calkyl claim 1 , or substituted or unsubstituted C-Ccycloalkyl.4. The composite material of claim 3 , wherein R claim 3 , R claim 3 , R claim 3 , and Rare independently H or substituted or unsubstituted C-Calkyl.5. The composite material of claim 3 , wherein the at least one ammonium cation comprises [HN(CH)].6. The composite material of claim 1 , wherein the at least one cation comprises a phosphonium cation of the structure PRRRR claim 1 , wherein R claim 1 , R claim 1 , R claim 1 , and Rare independently H claim 1 , halogen claim 1 , substituted or unsubstituted C-Calkyl claim 1 , substituted or unsubstituted C-Ccycloalkyl claim 1 , or wherein ...

Process for Producing Metallocenes

The present invention relates to an improved process for the preparation of metallocenes of the general formula (A) CR2L2MX2 as well as to intermediates useful in the synthesis of said metallocene and the use thereof as a catalyst in a polymerization of an olefin.

METHODS OF PRODUCING ALKYLFURANS

Provided herein are methods of producing dialkylfurans, such as 2,5-dimethylfuran, and other alkyl furans, such as 2-methylfuran. For example, 2,5-dimethylfuran may be produced by reducing (5-methylfuran-2-yl)methanol or 2-(chloromethyl)-5-methylfuran. 2. The method of claim 1 , wherein the basic solid support comprises a basic metal oxide.3. The method of claim 1 , wherein the basic solid support comprises a solid support modified by an alkali metal or an alkali earth metal.4. The method of claim 1 , wherein the basic solid support comprises a solid support modified by a base.5. The method of claim 1 , wherein the basic solid support comprises BeO claim 1 , MgO claim 1 , CaO claim 1 , SrO claim 1 , BaO claim 1 , ZnO claim 1 , AlO claim 1 , YO claim 1 , LaO claim 1 , CeO claim 1 , ThO claim 1 , TiO claim 1 , ZrOor SnO claim 1 , or any combinations thereof.739-. (canceled)4143-. (canceled) This application claims priority to U.S. Provisional Patent Application No. 62/037,806, filed Aug. 15, 2014, which is incorporated herein by reference in its entirety.The present disclosure relates generally to methods of producing dialkylfurans and other alkylfurans, and more specifically to methods of producing 2,5-dimethylfuran and 2-methylfuran.Dialkylfurans, such as 2,5-dimethylfuran (DMF), and other alkylfurans have potential applications for use as biofuels. Several methods are known in the art to produce 2,5-dimethylfuran. Current methods known in the art to produce 2,5-dimethylfuran from other furan compounds have been challenging with respect to minimizing the furan ring reduction. Thus, what is needed in the art are methods of selectively reducing furan compounds to produce 2,5-dimethylfuran and other alkylfurans.Provided herein are methods to reduce furan compounds to produce alkylfurans. In some aspects, provided is a method of producing a compound of formula (I′):wherein:wherein:In some embodiments, the compound of formula (A) is reduced to produce the compound of ...

Methods of Refining Natural Oil Feedstocks

Methods are provided for refining natural oil feedstocks. The methods comprise reacting the feedstock in the presence of a metathesis catalyst under conditions sufficient to form a metathesized product comprising olefins and esters. In certain embodiments, the methods further comprise separating the olefins from the esters in the metathesized product. In certain embodiments, the methods further comprise hydrogenating the olefins under conditions sufficient to form a fuel composition. In certain embodiments, the methods further comprise transesterifying the esters in the presence of an alcohol to form a transesterified product.

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 ...

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.

Octahydroanthracene Compound, Preparation Method and Application Thereof

An octahydroanthracene compound having the structure shown in formula (I) and (II), preparation method and application thereof are disclosed. The octahydroanthracene compound has a good therapeutic effect on tumors and neurodegenerative diseases. The preparation of the octahydroanthracene compound is mainly carried out by using benzene as a starting material, and being subjected to Friedel-Crafts reaction, nitration, reduction, (sulfo-) amide formation, reduction, urea formation or amide formation, thus obtaining a target compound. 2. The octahydroanthracene compound and the pharmaceutically acceptable salts of the octahydroanthracene compound of claim 1 , whereinthe Linker is a substituted/unsubstituted phenyl group, pyridine, furan, pyrrole, thiazole or thiophene; wherein a substituent of the substituted phenyl group, pyridine, furan, pyrrole, thiazole or thiophene is a C1-C6 alkyl group or a C1-C6 alkoxy group.3. The octahydroanthracene compound and the pharmaceutically acceptable salts of the octahydroanthracene compound of claim 1 , wherein the nitrogen-free structural fragment is C1-C10 alkyl group.5. The octahydroanthracene compound and the pharmaceutically acceptable salts of the octahydroanthracene compound of claim 1 , wherein X is hydrogen claim 1 , methyl or ethyl.6. An octahydroanthracene compound and pharmaceutically acceptable salts of the octahydroanthracene compound claim 1 , selecting from:4-[(1,1,4,4,5,5,8,8-octamethyl-1,2,3,4,5,6,7,8-octahydro-9-anthryl) carbamoyl] methyl benzoate;4-[(1,1,4,4,5,5,8,8-octamethyl-1,2,3,4,5,6,7,8-octahydro-9-anthryl) carbamoyl] benzoic acid;N-hydroxy-4-[(1,1,4,4,5,5,8,8-octamethyl-1,2,3,4,5,6,7,8-octahydro-9-anthryl) carbamoyl] benzamide;N-(2-aminophenyl)-4-[(1,1,4,4,5,5,8,8-octamethyl-1,2,3,4 5,6,7,8-octahydro-9-anthryl) carbamoyl] benzamide;N[2-(N,N-diethylamino)]ethyl-4-[(1,1,4,4,5,5,8,8-octamethyl-1,2,3,4,5,6,7,8-octahydro-9-anthryl) carbamoyl] benzamide;N-(2-amino) ethyl -4[(1,1,4,4,5,5,8,8-octamethyl-1,2,3,4,5 ...

Process for synthesis of indenes

The present invention relates to a new process for the synthesis of 2,3,4,5,6,7-substituted indenes, which are useful precursors for the formation of certain ansa-metallocene catalysts.

Surfactant-Enabled Transition Metal-Catalyzed Chemistry

In one embodiment, the present application discloses mixtures comprising (a) water in an amount of at least 1% wt/wt of the mixture; (b) a transition metal catalyst; and (c) one or more solubilizing agents; and methods for using such mixtures for performing transition metal mediated bond formation reactions. 114.-. (canceled)16. The method of claim 15 , wherein the transition metal mediated bond formation is performed in an aqueous solvent.17. The method of claim 15 , wherein the transition metal catalyst is selected from an organo-palladium or -nickel reagent claim 15 , organo-copper or -gold reagent claim 15 , organo-rhodium or -iridium complex claim 15 , or an organo-ruthenium claim 15 , -iron claim 15 , or -osmium reagent claim 15 , wherein the catalyst is capable of promoting cross-coupling reactions claim 15 , or other reactions characteristic of catalysis by these metals claim 15 , that form a carbon-carbon claim 15 , carbon-heteroatom or carbon-hydrogen bond.18. The method of claim 15 , wherein Yis methyl.19. The method of claim 15 , wherein the solubilizing agent is selected from the group consisting of Poloxamer 188 claim 15 , Polysorbate 80 claim 15 , Polysorbate 20 claim 15 , Vit E-TPGS claim 15 , Solutol HS 15 claim 15 , PEG-40 Hydrogenated castor oil (Cremophor RH40) claim 15 , PEG-35 Castor oil (Cremophor EL) claim 15 , PEG-8-glyceryl capylate/caprate (Labrasol) claim 15 , PEG-32-glyceryl laurate (Gelucire 44/14) claim 15 , PEG-32-glyceryl palmitostearate (Gelucire 50/13); Polysorbate 85 claim 15 , polyglyceryl-6-dioleate (Caprol MPGO) claim 15 , mixtures of high and low HLB emulsifiers; sorbitan monooleate (Span 80) claim 15 , Capmul MCM claim 15 , Maisine 35-1 claim 15 , glyceryl monooleate claim 15 , glyceryl monolinoleate claim 15 , PEG-6-glyceryl oleate (Labrafil M 1944 CS) claim 15 , PEG-6-glyceryl linoleate (Labrafil M 2125 CS) claim 15 , oleic acid claim 15 , linoleic acid claim 15 , propylene glycol monocaprylate (e.g. Capmul PG-8 or Capryol ...

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

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

Catalyst 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 the generation of 2,5-dimethylhexene from isobutene

A method of making one or more 2,5-dimethylhexenes is described. The method includes reacting isobutene with isobutanol in the presence of a platinum group metal catalyst to form one or more 2,5-dimethylhexenes. A method of making p-xylene using one or more 2,5-dimethylhexenes is also described. The p-xylene can be made from totally renewable sources, if desired.

CATALYSIS BY METAL NANOPARTICLES DISPERSED WITHIN A HIERARCHICALLY POROUS CARBON MATERIAL

Disclosed are hierarchically porous carbon materials with a plurality of discreet nanoparticles dispersed on their carbon phase. The materials possess a continuous network of pores that spans the porous material, permitting the flow of fluids into and through the material. The porous materials can be used as heterogeneous catalysts. 1. A hierarchically porous material comprising:a) a plurality of macropores defined by a wall, wherein the macropores have a diameter of from about 0.1 μm to about 50 μm,wherein the macropores interconnect, forming a continuous network of pores that spans the porous material,wherein the walls of the macropores comprise a plurality of mesopores defined by a wall, wherein the mesopores have a diameter of from about 2 nm to about 50 nm, andwherein the walls of the macropores and mesopores comprise a continuous carbon phase; andb) a plurality of discreet nanoparticles dispersed on the carbon phase of the macropores and mesopores.2. The material of claim 1 , wherein the material is a monolith.3. The material of claim 1 , wherein the material is a particle.4. The material of claim 1 , wherein the macropores have a diameter of from about 0.5 μm to about 30 μm.5. The material of claim 1 , wherein the mesopores having a diameter of from about 2 nm to about 15 nm thereby resulting in a porous material with hierarchical pores.6. The material of claim 1 , wherein the nanoparticles comprise a catalytically active metal claim 1 , metal oxide claim 1 , or combinations thereof.7. The material of claim 6 , wherein the metal claim 6 , metal oxide claim 6 , or combinations thereof comprise a metal selected from the group consisting of Ti claim 6 , V claim 6 , Cr claim 6 , Mn claim 6 , Fe claim 6 , Co claim 6 , Ni claim 6 , Cu claim 6 , Zr claim 6 , Nb claim 6 , Mo claim 6 , Tc claim 6 , Ru claim 6 , Rh claim 6 , Pd claim 6 , Ag claim 6 , Hf claim 6 , Ta claim 6 , W claim 6 , Re claim 6 , Os claim 6 , Ir claim 6 , Pt claim 6 , Au claim 6 , La claim 6 , Ce ...

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 ...

Spiroketal-Based C2-Symmetric Scaffold For Asymmetric Catalysis

Provided herein is a compound of formula (I): 4. The compound of claim 1 , wherein at least one X is OH.5. (canceled)6. The compound of claim 1 , wherein at least one X is PAr.7. (canceled)8. The compound of claim 1 , wherein at least one X is OPAr.9. (canceled)10. The compound of claim 1 , wherein at least one X is P(O)Ar.1112.-. (canceled)13. The compound of claim 6 , wherein Ar comprises phenyl.14. The compound of claim 1 , wherein both X together form OPNR′.1518.-. (canceled)19. The compound of claim 14 , wherein R′ is methyl.2022.-. (canceled)23. The compound of claim 1 , wherein R is ethyl.2428.-. (canceled)29. The compound of claim 1 , wherein at least one R is 3-10 membered heterocycloalkyl having 1-4 heteroatoms independently selected from N claim 1 , O claim 1 , and S.3034.-. (canceled)36. A catalyst comprising the compound of formula (I) according to and a transition metal.37. The catalyst of claim 36 , wherein the transition metal comprises iridium claim 36 , palladium claim 36 , rhodium claim 36 , platinum claim 36 , copper claim 36 , nickel claim 36 , cobalt claim 36 , or gold.38. A method of preparing the catalyst of comprising admixing the compound of formula (I) and the transition metal to form the catalyst.39. (canceled)40. The method of claim 38 , wherein the transition metal comprises [Ir(COD)Cl] claim 38 , [Pd(allyl)Cl] claim 38 , or Pd(dba).41. The method of claim 38 , wherein the compound of formula (I) and the transition metal are provided in a molar ratio of about 6:1 to 1:1.42. A method comprising:{'claim-ref': {'@idref': 'CLM-00036', 'claim 36'}, 'admixing a first reactant, a second reactant, and the catalyst of under conditions sufficient to allow reaction of the first reactant and the second reactant to form a reaction product, wherein the reaction product comprises a chiral center and the reaction produces an enantiomeric excess (ee) of the reaction product.'}43. The method of claim 42 , wherein the reaction comprises a hydroarylation ...

Conversion of Non-Aromatic Hydrocarbon

Systems and methods are provided for converting alkane while generating improved yields of desirable aromatics and/or improved selectivity for forming desired aromatics, such as para-xylene (p-xylene). Aromatics generated during the aromatic formation process can be alkylated to form xylenes with improved yield and/or improved selectivity. 1. A method for forming aromatic compounds , comprising:providing a feed comprising non-aromatic hydrocarbon;{'sub': 7', '8, "producing an aromatic formation effluent comprising benzene, Caromatic hydrocarbon, and ≦20 wt. % of Caromatic hydrocarbon from at least a portion of the feed's non-aromatic hydrocarbon in an aromatic formation process carried out under effective aromatic formation conditions;"}{'sub': 8', '8', '8', '7', '6', '7, 'separating from the aromatic formation effluent a first Cintermediate stream and a first lower boiling intermediate stream, the first Cintermediate stream having a Caromatic hydrocarbon concentration (weight percent) greater than that of the aromatic formation effluent, the first lower boiling intermediate stream having a benzene concentration (weight percent), a Caromatic hydrocarbon concentration (weight percent), or a combined C-Caromatic hydrocarbon concentration (weight percent) greater than those of the aromatic formation effluent;'}{'sub': '8', 'reacting at least a portion of the first lower boiling intermediate stream with a methylating agent in the presence of a zeolite catalyst to form a methylated intermediate stream, the methylated intermediate stream having a Caromatic hydrocarbon concentration (weight percent) greater than that of the portion of the first lower boiling intermediate stream which reacts to form the methylated intermediate stream;'}{'sub': 8', '8', '8, 'separating from the methylated intermediate stream a second Cintermediate stream and a second lower boiling intermediate stream, the second Cintermediate stream having a Caromatic hydrocarbon concentration (weight ...

Low system memory detection

Methods, systems, and computer readable media may be operable to facilitate an anticipation of an execution of a process termination tool. An allocation stall counter may be queried at a certain frequency, and from the query of the allocation stall counter, a number of allocation stall counter increments occurring over a certain duration of time may be determined. If the number of allocation stall counter increments is greater than a threshold, a determination may be made that system memory is running low and that an execution of a process termination tool is imminent. In response to the determination that system memory is running low, a flag indicating that system memory is running low may be set, and one or more programs, in response to reading the flag, may free memory that is not necessary or required for execution.

Process for the Production of Xylenes

In a process for producing para-xylene, a feed stream comprising C aromatic hydrocarbons is separated into a Caromatic hydrocarbon-containing stream, a Caromatic hydrocarbon-containing stream, and a C aromatic hydrocarbon-containing stream. The C aromatic hydrocarbon-containing stream is contacted with a methylating agent to convert toluene to xylenes and produce a methylated effluent stream. Ethylbenzene is removed from the Caromatic hydrocarbon-containing stream, para-xylene is recovered from the ethylbenzene-depleted Caromatic hydrocarbon-containing stream and the methylated effluent stream in a para-xylene recovery section to produce a para-xylene depleted stream, which is then contacted with a xylene isomerization catalyst under liquid phase conditions effective to isomerize xylenes in the para-xylene depleted stream and produce an isomerized stream. The C-containing stream with a transalkylation catalyst under conditions effective to convert C-aromatics to C-aromatics and produce a transalkylated stream, which is recycled together with the isomerized stream to the para-xylene recovery section.

METHOD AND APPARATUS FOR CAPTURING AND SEQUESTERING CARBON

A method for converting carbon dioxide (CO2) into useful carbonaceous compounds includes the steps of recovering CO2 from a CO2 emitting source, passing the recovered CO2 through a CO2 stripper, and using CO2 passed through the CO2 stripper as feedstock for reactions that generate useful carbonaceous compounds. The method further reduces CO2 emissions by preparing CO2 to be used as feedstock to drive other beneficial reactions. 1. A method for converting carbon dioxide (CO2) into useful carbonaceous compounds , comprising:recovering CO2 from a CO2 emitting source;passing the recovered CO2 through a CO2 stripper; andusing CO2 passed through the CO2 stripper as feedstock for reactions that generate useful carbonaceous compounds.2. The method of claim 1 , wherein the CO2 emitting source is an electric generating unit (EGU).3. The method of claim 1 , wherein CO2 is recovered by passing vent gas from an electric generating unit through an amine scrubber.4. The method of claim 3 , wherein the recovered CO2 is a vapor.5. The method of claim 4 , wherein the CO2 vapor further comprises water vapor.6. The method of claim 1 , wherein the useful carbonaceous compounds are synthesis gas claim 1 , gasoline claim 1 , methanol claim 1 , ethylene claim 1 , alkane hydrocarbons claim 1 , acetic acid claim 1 , magnesite claim 1 , silicic acid claim 1 , or silica.7. The method of claim 6 , wherein the alkane hydrocarbons are diesel fuel.8. A method for producing gasoline claim 6 , comprising:diverting CO2 from an electric generating unit to an amine scrubber to generate a CO2-rich amine absorber fluid;flowing the CO2-rich amine absorber fluid to a dry reformer; andmixing the CO2-rich amine absorber fluid in the dry reformer with methane and steam to yield a synthesis gas.9. The method of claim 8 , wherein the synthesis gas has a hydrogen to carbon ratio of about 2 to about 4.10. The method of claim 8 , wherein the synthesis gas has a hydrogen to carbon ratio of about 2 to about 3.11. ...

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 ...

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

Apparatuses and processes for converting an oxygenate feedstock, such as methanol and/or 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 olefins 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; andd. separating olefins 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 500° F. to about 1100° F.3. The process of claim 1 , wherein the pressure in the fluidized bed reactor is about 3 psig to about 450 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. A process for converting an oxygenate feedstock to aromatics 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 ...

MULTIFUNCTIONAL POROUS ARAMIDS (AEROGELS), FABRICATION THEREOF, AND CATALYTIC COMPOSITIONS DERIVED THEREFROM

The present disclosure provides a series of new and improved porous polyamide aerogels derived from multifunctional aromatics that combine the high mechanical strength of aramids with the pore structure of aerogels. The polyamide aerogels have a hyperbranched structure, relatively low density, high porosity and may be derived from functionalized monomers having more aromatic groups than functional groups. The present disclosure also provides a new method for producing the porous polyamide aerogels by polymerizing an aromatic multifunctional carboxylic acid or a ferrocene multifunctional carboxylic acid with a polyfunctional aromatic isocyanate at moderate reaction conditions followed by drying with liquid CO. Also disclosed are various methods of use of these polyamide aerogels in a variety of applications, particularly in the generation of various precious metal catalysts. Thus, monolithic nanoporous carbon-supported Fe, Au, Pt, Pd, Co, Ni, Ru, and Rh catalysts are disclosed herein, which are derived by pyrolysis and transmetalation via galvanic replacement of ferrocene-based polyamide aerogels. 3. A process for carbonizing the polymeric aerogel of claim 1 , said process comprising the step of pyrolizing the polymeric aerogel at temperatures in the range 500-2300° C. to yield a nanoporous product that includes iron-doped carbon-monoliths containing Fe(0) nanoparticles in graphitic pockets dispersed throughout the 3D matrix of monolithic nanoporous carbon.4. A process for partially or completely transmetalating the iron-doped carbon-monoliths of to produce M-doped carbon monoliths claim 3 , wherein M is one or more metals selected from the group of metals consisting of Fe claim 3 , Au claim 3 , Pt claim 3 , Pd claim 3 , Co claim 3 , Ni claim 3 , Ru claim 3 , and Rh claim 3 , said process comprising the step of dipping the iron-doped carbon monoliths in solutions of the respective metal ions.5. The process of claim 4 , further including the step of subjecting the ...

FULLERENE DERIVATIVES, AND RELATED MATERIALS, METHODS AND DEVICES

The invention relates to improved fullerene derivatives, to methods for their synthesis and any educts or intermediates used in such methods, to compositions and formulations containing fullerene derivatives, to the use of the fullerene derivatives, compositions and formulations in, or for the preparation of, organic electronic (OE) devices like for example organic photovoltaic (OPV) devices or organic photodetectors (OPD), and to OE, OPV and OPD devices comprising, or being prepared from, these fullerene derivatives, compositions or formulations. 2. The compound of claim 1 , wherein one or more of R claim 1 , R claim 1 , R claim 1 , R claim 1 , R claim 1 , R claim 1 , Rand Rdenote H.3. The compound of claim 1 , wherein Rand Rare different from H and Rand Rdenote H claim 1 , or Rand Rare different from H and Rand Rdenote H.4. The compound according to claim 1 , wherein those groups R claim 1 , R claim 1 , Rand Rwhich are different from H denote a straight-chain claim 1 , branched or cyclic alkyl group with 1 to 50 C atoms claim 1 , in which one or more CHgroups are optionally replaced by —O— claim 1 , —S— claim 1 , —C(═O)— claim 1 , —C(═S)— claim 1 , —C(═O)—O— claim 1 , —O—C(═O)— claim 1 , —S(O)— claim 1 , —NR— claim 1 , —SiRR— claim 1 , —CF— claim 1 , —CHR═CR— claim 1 , —CY═CY— or —C≡C— in such a manner that O and/or S atoms are not linked directly to one another claim 1 , one or more CHor CHgroups are optionally replaced by a cationic group or an anionic group claim 1 , and one or more H atoms are optionally replaced by F claim 1 , Cl claim 1 , Br claim 1 , I or CN claim 1 , and wherein{'sup': 0', '00', '1', '2, 'Rand Rdenote H or an optionally substituted carbyl or hydrocarbyl group with 1 to 40 C atoms, and Yand Yare independently of each other H, F, Cl or CN.'}5. (canceled)6. The compound according to claim 1 , wherein those groups R claim 1 , R claim 1 , Rand Rwhich are different from H denote an alkyl claim 1 , alkoxy claim 1 , thioalkyl claim 1 , ...

PROCESS FOR THE AROMATIZATION OF A METHANE-CONTAINING GAS STREAM

A process is disclosed for making styrene and/or ethylbenzene by reacting toluene with a Csource over a catalyst in at least one radial reactor to form a product stream comprising styrene and/or ethylbenzene. 1. A process for making styrene comprising:{'sub': '1', 'reacting toluene with a Csource over a catalyst in at least one radial reactor to form a product stream comprising styrene.'}2. The process of claim 1 , wherein the Csource is selected from the group consisting of methanol claim 1 , formaldehyde claim 1 , formalin claim 1 , trioxane claim 1 , methylformcel claim 1 , paraformaldehyde claim 1 , methylal claim 1 , dimethyl ether claim 1 , and combinations thereof.3. The process of claim 1 , wherein the reaction pressure in the radial reactor is in the range of 0.1 atm to 70 atm.4. The process of claim 1 , wherein the reaction pressure in the radial reactor is in the range of about 0.1 atm to about 10 atm.5. The process of claim 1 , wherein the radial reactor comprises a reaction zone comprising the catalyst claim 1 , wherein the process is conducted such that the average residence time in the reaction zone of the reactants is less than about 10 minutes.6. The process of claim 1 , wherein the radial reactor comprises a reaction zone comprising the catalyst claim 1 , wherein the process is conducted such that the average residence time in the reaction zone of the reactants is less than about 5 minutes.7. The process of claim 1 , wherein the radial reactor comprises a reaction zone comprising the catalyst claim 1 , wherein the process is conducted such that the average residence time in the reaction zone of the reactants is less than about 30 seconds.8. The process of claim 1 , wherein the catalyst is based on a zeolite selected from the group consisting of faujasites.9. The process of claim 8 , wherein the catalyst is based on an X-type zeolite.10. The process of claim 1 , wherein the catalyst is promoted with a promoter selected from the group consisting of ...

Method for producing fullerene derivative

(in formula (1), C* are each carbon atoms adjacent to each other for forming a fullerene skeleton, A is a linking group having 1-4 carbon atoms for forming a ring structure with two C*, in which a portion thereof may be a substituted or condensed group).

Process for Producing Paraxylene by Methylation of Benzene and/or Toluene

A process is described for producing paraxylene, in which an aromatic hydrocarbon feedstock comprising benzene and/or toluene is contacted with an alkylating reagent comprising methanol and/or dimethyl ether in an alkylation reaction zone under alkylation conditions in the presence of an alkylation catalyst to produce an alkylated aromatic product comprising xylenes. The alkylation catalyst comprises a molecular sieve having a Constraint Index≤5, and the alkylation conditions comprise a temperature less than 500° C. Paraxylene may then be recovered from the alkylated aromatic product.

PROCESS FOR CONVERSION OF METHANE TO HIGHER HYDROCARBONS, INCLUDING LIQUID FUELS

Aspects of the invention are associated with the discovery of processes for converting methane (CH), present in a methane-containing feedstock that may be obtained from a variety of sources such as natural gas, to higher hydrocarbons (e.g., C hydrocarbons) such as gasoline, diesel fuel, or jet fuel boiling-range hydrocarbons, which may optionally be separated (e.g., by fractionation) for use as transportation fuels, or otherwise as blending components for such fuels. Particular aspects of the invention are associated with advantages arising from maintaining reaction conditions that improve the yield of C hydrocarbons. Further aspects relate to the advantages gained by integration of the appropriate reactions to carry out the methane conversion, with downstream separation to recover and recycle desirable components of the reaction effluent, thereby improving process economics to the extent needed for commercial viability. 1. A process for converting a methane-containing feedstock to C hydrocarbons , the process comprising feeding at least a portion of the methane-containing feedstock to a hydrogenation/oligomerization reactor to suppress a methane re-formation reaction and thereby increase a selectivity or yield of the C hydrocarbons , in an oligomerization effluent of the hydrogenation/oligomerization reactor , from oligomerization of CS.2. The process of claim 1 , further comprising recycling a recycle gas stream comprising both CHand HS to a sulfur oxidation reactor positioned upstream of the hydrogenation/oligomerization reactor claim 1 , wherein the recycle gas stream comprises at least a portion of an HS/CHstream that is separated from a vapor product of the oligomerization effluent.3. The process of claim 1 , further comprising recycling claim 1 , to the hydrogenation/oligomerization reactor claim 1 , at least a portion of a hydrogen product stream that is separated from a vapor product of the oligomerization effluent.4. A process for converting a methane- ...

PROCESS TO PRODUCE PARAFFINIC HYDROCARBON FLUIDS FROM LIGHT PARAFFINS

A process for converting light paraffins to heavier paraffinic hydrocarbon fluids is disclosed. The process involves: (1) oxidation of iso-paraffins to alkyl hydroperoxides and alcohols; (2) conversion of the alkyl hydroperoxides and alcohols to dialkyl peroxides; and (3) radical-initiated coupling of paraffins and/or iso-paraffins using the dialkyl peroxides as radical initiators, thereby forming heavier hydrocarbon products. Fractionation of the heavy hydrocarbon products can then be used to isolate fractions for use as hydrocarbon fluids. 1. A process for the conversion of paraffins to paraffinic hydrocarbon fluids , comprising:a) oxidizing iso-paraffins from a first paraffinic feed with air or oxygen to form alkyl hydroperoxides and alcohols;b) catalytically converting the alkyl hydroperoxides and alcohols to dialkyl peroxides; andc) coupling a second paraffinic feed using the dialkyl peroxides as radical initiators to create hydrocarbon fluids.2. The process of claim 1 , wherein the first paraffinic feed comprises normal paraffins claim 1 , iso-paraffins claim 1 , or mixtures thereof.3. The process of claim 2 , further comprising isomerizing at least a fraction of the normal paraffins to iso-paraffins prior to step (a).4. The process of claim 1 , wherein the second paraffinic feed comprises normal paraffins claim 1 , iso-paraffins claim 1 , or mixtures thereof.5. The process of claim 1 , further comprising fractionating the paraffinic hydrocarbon fluids to isolate a desired fraction.6. The process of claim wherein the first paraffinic feed and the second paraffinic feed are independently selected from normal paraffins with 4 or 5 carbon numbers claim 1 , iso-paraffins with 4 or 5 carbon numbers claim 1 , and mixtures thereof.7. The process of claim 1 , wherein the iso-paraffins of step (a) are selected from iso-butane claim 1 , iso-pentane claim 1 , and mixtures thereof.8. The process of claim 1 , wherein the iso-paraffins of step (a) comprise 60 to 99 wt % iso ...

INTEGRATED PROCESS FOR MAKING HIGH-OCTANE GASOLINE

An integrated process for converting low-value paraffinic materials to high octane gasoline and high-cetane diesel light is disclosed. The process involves: (1) oxidation of an iso-paraffin to alkyl hydroperoxide and alcohol; (2) converting the alkyl hydroperoxide and alcohol to dialkyl peroxide; (3) converting low-octane, paraffinic gasoline molecules using the dialkyl peroxides as radical initiators, thereby forming high-cetane diesel, while the dialkyl peroxide is converted to an alcohol; (4) converting the alcohol to an olefin; and (5) alkylating the olefin with iso-butane to form high-octane alkylate. The net reaction is thus conversion of iso-paraffin to high-octane gasoline alkylate, and conversion of low-octane paraffinic gasoline to high-cetane diesel. 1. A process for upgrading substantially paraffinic feed to high-cetane diesel , comprising:(a) oxidizing a first feed stream comprising one or more iso-paraffins to form alkyl hydroperoxides and first alcohols;(b) catalytically converting the alkyl hydroperoxides and first alcohols to dialkyl peroxides; and(c) coupling a second feed stream substantially comprising paraffins using the dialkyl peroxides as a radical initiator to create high-cetane diesel and second alcohols.2. The process of claim 1 , wherein the first feed stream comprises iso-butane.3. The process of claim 1 , wherein the second feed stream comprises heavy virgin naphtha.4. The process of claim 1 , wherein the second feed stream comprises heavy cat naphtha.5. The process of claim 1 , wherein the second feed stream comprises coker naphtha.6. The process of claim 1 , wherein the second feed stream comprises paraffins in the carbon number range of 7-12.7. The process of claim 1 , further comprising converting the second alcohols to olefins.8. The process of claim 7 , further comprising alkylating the olefins with iso-paraffins to form high-octane gasoline.9. The process of claim 7 , further comprising dimerizing the olefins to form high octane ...

High octane gasoline and process for making same

A process for converting light paraffins to a high octane gasoline composition is disclosed. The process involves: (1) oxidation of iso-paraffins to alkyl hydroperoxides and alcohol; (2) conversion of the alkyl hydroperoxides and alcohol to dialkyl peroxides; and (3) radical coupling of iso-paraffins using the dialkyl peroxides as radical initiators, thereby forming gasoline-range molecules. Fractionation of the gasoline-range molecules can then be used to isolate high octane gasoline fractions having a road octane number [(RON+MON)/2] greater than 110.

METHOD FOR FORMING CARBON-CARBON BOND

A method for forming a carbon-carbon bond, wherein a reaction is performed by filling a platinum group metal-supported catalyst into a filling container, and passing a raw material liquid through the platinum group metal-supported catalyst in a continuous circulation manner, and wherein the platinum group metal-supported catalyst is a platinum group metal-supported catalyst in which nanoparticles of a platinum group metal with an average particle diameter of 1 to 100 nm are supported on a non-particulate organic porous ion exchanger formed of a continuous framework phase and a continuous pore phase. 1. A method for forming a carbon-carbon bond to form a carbon-carbon bond by performing (1) reaction of an aromatic halide with an organoboron compound , (2) reaction of an aromatic halide with a compound having a terminal alkynyl group , or (3) a reaction of an aromatic halide with a compound having an alkenyl group ,wherein the carbon-carbon bond-forming reaction is performed by introducing a raw material liquid (i) containing the aromatic halide and the organoboron compound, a raw material liquid (ii) containing the aromatic halide and the compound having a terminal alkynyl group, or a raw material liquid (iii) containing the aromatic halide and the compound having an alkenyl group, through an introduction path of a filling container filled with a platinum group metal-supported catalyst, into the filling container, passing the raw material liquid through the platinum group metal-supported catalyst, and discharging the reaction liquid from a discharge path of the filling container, andwherein the platinum group metal-supported catalyst is a platinum group metal-supported catalyst in which nanoparticles of a platinum group metal with an average particle diameter of 1 to 100 nm are supported on a non-particulate organic porous ion exchanger, and the non-particulate organic porous ion exchanger is formed of a continuous framework phase and a continuous pore phase; has a ...

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.

MULTIFUNCTIONAL POROUS ARAMIDS (AEROGELS) AND FABRICATION THEREOF

The present disclosure provides a series of new and improved porous polyamide aerogels derived from multifunctional aromatics that combine the high mechanical strength of aramids with the pore structure of aerogels. The polyamide aerogels have a hyperbranched structure, relatively low density, high porosity and may be derived from functionalized monomers having more aromatic groups than functional groups. The present disclosure also provides a new method for producing the porous polyamide aerogels by polymerizing an aromatic multifunctional carboxylic acid or a ferrocene multifunctional carboxylic acid with a polyfunctional aromatic isocyanate at moderate reaction conditions followed by drying with liquid CO. Also disclosed are various methods of use of these polyamide aerogels in a variety of applications. 2. The ferrocene carboxamide aerogel of having a hyperbranched structure.4. The ferrocene carboxamide aerogel of claim 3 , in which each of the linking bonds on the phenyl rings is attached at the 4-position of its respective phenyl ring.7. The ferrocene carboxamide aerogel of claim 6 , in which each of the linking bonds on the phenyl rings is attached at the 4-position of its respective phenyl ring.8. The ferrocene carboxamide aerogel of obtained by the reaction of 1 claim 6 ,1′-ferrocene dicarboxylic acid with a tris(isocyanato) compound of the formula G(N═C═O) claim 6 , followed by decarboxylation; wherein G represents a group as defined in .9. The ferrocene carboxamide aerogel of wherein the tris(isocyanato) compound is tris(4-isocyanatophenyl)methane.10. A method for producing a polymeric ferrocene carboxamide aerogel comprising the reaction step of mixing together a multifunctional ferrocene carboxylic acid and a polyfunctional aromatic isocyanate in an anhydrous aprotic solvent.11. The method of wherein the polyfunctional aromatic isocyanate is tris(4-isocyanatophenyl)methane.12. The method of wherein the multifunctional ferrocene carboxylic acid is 1 ...

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

A turbulent 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. The turbulent fluidized bed reactor includes a first reactor feed distributor and a number of second reactor feed distributors; the first reactor feed distributor and the plurality of second reactor feed distributions are sequentially arranged. 126-. (canceled)27. A turbulent fluidized bed reactor for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene , the turbulent fluidized bed reactor comprising 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 turbulent fluidized bed reactor; andthe number of the second reactor feed distributors is in a range from 2 to 10.28. The turbulent fluidized bed reactor of claim 27 , the turbulent fluidized bed reactor further comprises a first reactor gas-solid separator and a second reactor gas-solid separator claim 27 , the first reactor gas-solid separator is placed in a dilute phase zone or outside a reactor shell claim 27 , and the second reactor gas-solid separator is placed in the dilute phase zone or outside the reactor ...

TRIALKYLPHOSPHONIUM IONIC LIQUIDS, METHODS OF MAKING, AND ALKYLATION PROCESSES USING TRIALKYLPHOSPHONIUM IONIC LIQUIDS

A trialkylphosphonium haloaluminate compound having a formula: 2. The process of wherein R claim 1 , R claim 1 , and Rare Cto Chydrocarbyl.3. The process of wherein R claim 1 , R claim 1 , and Rhave the same number of carbon atoms.4. The process of wherein R claim 1 , R claim 1 , and Rare identical.5. The process of wherein each of R claim 4 , R claim 4 , and Ris selected from the group consisting of methyl claim 4 , ethyl claim 4 , propyl claim 4 , butyl claim 4 , pentyl claim 4 , and hexyl.6. The process of wherein the trialkylphosphonium haloaluminate compound comprises tri-n-butylphosphonium AlCl— claim 5 , tri-isobutylphosphonium AlCl— claim 5 , or di-n-butyl-sec-butylphosphonium AlCl—.7. The process of wherein an initial kinematic viscosity of the trialkylphosphonium ionic liquid catalyst composition is less than about 70 cSt at 25° C.8. The process of wherein a molar ratio of aluminum to phosphorous in the ionic liquid catalyst composition is in the range of 1.8 to 2.2.10. The process of wherein the trialkylphosphonium ionic liquid catalyst composition further comprises a co-catalyst.11. The process of wherein the co-catalyst comprises a Brønsted acid selected from the group consisting of HCl claim 10 , HBr claim 10 , HI claim 10 , and mixtures thereof claim 10 , or a Brønsted acid precursor.12. The process of further comprising:separating the alkylate and unreacted isoparaffin feed from the trialkylphosphonium ionic liquid catalyst composition to form a hydrocarbon stream comprising the alkylate and the unreacted isoparaffin feed and an ionic liquid stream comprising the trialkylphosphonium ionic liquid catalyst composition;separating the hydrocarbon stream into an alkylate stream and an unreacted isoparaffin stream; andrecycling at least one of the unreacted isoparaffin stream and the ionic liquid stream.13. The process of further comprising:regenerating at least a portion of the trialkylphosphonium ionic liquid catalyst composition in the ionic liquid ...

PROCESS AND APPARATUS FOR THE CONVERSION OF HYDROCARBONS

A hydrocarbon conversion process is described. The process includes contacting in a reactor an inert gas with one or more catalyst compositions suitable for methylation of toluene and hydrogenation of phenol; contacting a reducing agent with the one or more catalyst compositions under conditions suitable for reducing metal oxide content of the catalyst composition; contacting at least part of toluene and/or benzene-containing with a oxygenate in the presence of the one or more catalyst compositions and under conditions effective to convert toluene to xylenes and produce a reactor effluent stream comprising para-xylene and having a lower concentration of phenol than the toluene-containing stream; separating at least one para-xylene-enriched stream from the reactor effluent stream; and separating from the at least one para-xylene enriched stream at least one toluene-enriched stream and at least one para-xylene-product stream. An apparatus for carrying out such a process is also described. 1. A hydrocarbon conversion , comprising:a) contacting in at least a first reactor an inert gas with one or more catalyst compositions suitable for methylation of toluene and/or hydrogenation of phenol;b) contacting a reducing agent with the one or more catalyst compositions under conditions suitable for reducing metal oxide content of the first catalyst composition;c) contacting at least part of an aromatic hydrocarbon stream comprising ≧5.0 wt % toluene and/or benzene with a oxygenate in the presence of the first catalyst composition and under conditions effective to convert toluene to xylenes and produce a reactor effluent stream comprising para-xylene and having a lower concentration of phenol than the aromatic hydrocarbon stream;d) separating in a first separator at least one para-xylene-enriched stream from the reactor effluent stream; ande) separating in a second separator from the at least one para-xylene enriched stream at least one toluene-enriched stream and at least one ...

Method of Making Aromatic Hydrocarbons

A method for the purification of an aromatic hydrocarbon process stream having phenol therein is disclosed. Aspects of the method include contacting at least a portion of the aromatic hydrocarbon process stream with a hydrogenation catalyst under hydrogenation conditions to provide a hydrogenation effluent having a lower concentration of phenol than said aromatic hydrocarbon process stream. 1. A method for the purification of an aromatic hydrocarbon process stream comprising paraxylene and phenol , the method comprising contacting at least a portion of the aromatic hydrocarbon process stream with a hydrogenation catalyst under hydrogenation conditions to provide a hydrogenation effluent having a lower concentration of phenol than said aromatic hydrocarbon process stream.2. The method according to claim 1 , wherein the hydrogenation effluent comprises ≧25.0 wt % paraxylene.3. The method according to claim 1 , wherein said aromatic hydrocarbon process stream comprises an alkylation process effluent comprising the products of a reaction of an oxygenate with toluene and/or benzene in the presence of an alkylation catalyst under alkylation conditions to provide said aromatic hydrocarbon process stream claim 1 , wherein said oxygenate is selected from the group consisting of methanol claim 1 , dimethyl ether claim 1 , and mixtures thereof.4. The method according to claim 1 , wherein said aromatic hydrocarbon process stream is produced by the reaction of toluene and/or benzene with an oxygenate in the presence of an alkylation catalyst combined with the hydrogenation catalyst claim 1 , wherein said aromatic hydrocarbon process stream comprises ≧25.0 wt % paraxylene claim 1 , and wherein said oxygenate is selected from the group consisting of methanol claim 1 , dimethyl ether claim 1 , and mixtures thereof.5. The method of claim 1 , further including providing a hydrogen source capable of hydrogenating the phenol in the presence of the hydrogenation catalyst.6. The method ...

Method for Making a Catalyst Comprising a Phosphorous Modified Zeolite and Use of Said Zeolite

A method to make a phosphorus modified zeolite can include providing a zeolite having at least one ten member ring, making an ion-exchange, steaming the zeolite, and introducing phosphorus on the zeolite. The zeolite can be mixed with one or more binders and shaping additives, and then shaped. A metal can be introduced, and the catalyst can be washed, calcined, and steamed in an equilibration step. The steaming can be at performed at a steam severity (X) of at least about 2. The steaming can be performed at a temperature above 625° C. The catalyst can be used in alcohol dehydration, olefin cracking, MTO processes, and alkylation of aromatics by alcohols with olefins and/or alcohols. 1. Method to make a phosphorus modified zeolite comprising the following steps in this order ,a) providing a zeolite comprising at least one ten members ring in the structure, optionally making an ion-exchange,b) steaming said zeolite,c) introducing phosphorus on the zeolite to introduce at least 0.1 wt % of phosphorus, said introduction being made by dry impregnation or chemical vapor deposition,d) mixing said zeolite of step c) with at least a component selected among one or more binders and shaping additives,e) shaping said mixture,f) optionally introducing a metal, optionally simultaneously with step d),g) optionally washing the catalyst,h) optionally calcinating the catalyst,i) steaming the catalyst, also referred to as the equilibration step.2. Method according to wherein the phosphorus introduction of step c) is made by incipient wetness (IW) or incipient wetness impregnation (IWI).3. Method according to or wherein the steaming of step i) is performed in the range 420 to 870° C.4. Method according to wherein the steaming of step i) is performed in the range 480 to 870° C.5. Method according to wherein the steaming of step i) is performed in the range 625 to 870° C.6. Method according to wherein the steaming of step i) is performed in the range 700 to 800° C.7. Method according to ...

ALKYLATING PROCESS FOR ALKYL BENZENES

This invention relates to an alkylating process for alkyl benzenes, including the steps of: a) an alkyl benzene and a first stream of alkylating agent being fed into a first reaction zone, contacting with a catalyst A, to produce a process stream I; b) the process stream I and a second stream of alkylating agent being fed into at least one second reaction zone, contacting with a catalyst B, to produce a process stream II; and c) the process stream II being fed into at least one third reaction zone, contacting with a catalyst C, to produce a process stream III containing an alkylate. The present alkylating process can improve the utilization efficiency of the alkylating agent. 2. The alkylating process according to claim 1 , wherein in the first reaction zone claim 1 , the reaction temperature is 320-400 degrees centigrade claim 1 , the weight hourly space velocity (WHSV) is 2-4 h-1 claim 1 , the reaction pressure is 0-0.5 MPa (gage pressure); in the second reaction zone claim 1 , the reaction temperature is 380-420 degrees centigrade claim 1 , the weight hourly space velocity (WHSV) is 2-4 h-1 claim 1 , the reaction pressure is 0-0.5 MPa (gage pressure); in the third reaction zone claim 1 , the reaction temperature is 400-450 degrees centigrade claim 1 , the weight hourly space velocity (WHSV) is 2-4 h-1 claim 1 , the reaction pressure is 0-0.5 MPa (gage pressure); the ratio by molar of the alkyl benzene to the first stream of alkylating agent is greater than 1 but not greater than 6 claim 1 , and the ratio by molar of the alkyl benzene contained in the process stream I to the second stream of alkylating agent is 1-5.3. The alkylating process according to claim 2 , wherein the reaction temperature in the first reaction zone is less than the reaction temperature in the third reaction zone.4. The alkylating process according to claim 2 , wherein the ratio by molar of the alkyl benzene to the first stream of alkylating agent is greater than the ratio by molar of the ...

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 ...

Delaminated Zeolite Catalyzed Aromatic Alkylation

Provided is a method of alkylating an aromatic compound comprising contacting an aromatic compound and an alkylating agent in the presence of UCB-3 as a catalyst under reaction conditions suitable for aromatic alkylation. The aromatic compound preferably comprises benzene or toluene and the alkylation agent preferably comprises an olefin or alcohol. Lower temperature ranges can be used for the reaction, for example in the range of from 100 to 300° C. 1. A method of alkylating an aromatic compound comprising contacting an aromatic compound and an alkylating agent in the presence of UCB-3 as a catalyst under reaction conditions suitable for aromatic alkylation.2. The method of claim 1 , wherein the aromatic compound comprises benzene claim 1 , toluene claim 1 , or a mixture thereof.3. The method of claim 1 , wherein the aromatic compound comprises toluene.4. The method of claim 1 , wherein the alkylation agent comprises an alkane claim 1 , olefin or an alcohol.5. The method of claim 4 , wherein the alkylating agent comprises an olefin.6. The method of claim 5 , wherein the olefin comprises ethylene or propylene.7. The method of claim 3 , wherein the alkylating agent comprises propylene.8. The method of claim 4 , wherein the alkylating agent comprises an alcohol.9. The method of claim 8 , wherein the alkylating agent comprises methanol.10. The method of claim 3 , wherein the alkylating agent comprises methanol.11. The method of claim 8 , wherein the alkylating agent comprises isopropanol.12. The method of claim 3 , wherein the alkylating agent comprises isopropanol.13. The method of claim 1 , wherein the contacting is at a temperature in the range of 0° to 500° C.14. The method of claim 13 , wherein the contacting is at a temperature in the range of 150 to 250° C.15. The method of claim 13 , wherein the contacting is at a pressure in the range of 0.2 to 250 atm.16. The method of claim 1 , wherein the aromatic compound comprises benzene.17. The method of claim 16 , ...

METHOD FOR PREPARING ZSM-5 ZEOLITE

The present invention relates to a method for preparing ZSM-5 zeolite. The present invention can provide a method for preparing ZSM-5 zeolite comprising the steps of: preparing a first solution in a solution state by heating a mixture comprising a silica source, an alumina source, a neutralizing agent and a crystalline ZSM-5 nucleus; preparing a reaction mother liquid by mixing a second solution comprising salts into the first solution; and continuously crystallizing by continuously supplying the reaction mother liquid to a hydrothermal synthesis reactor, wherein formula [1] below is satisfied. 1. A method for preparing ZSM-5-based zeolite , the method comprising:heating a mixture including a silica source, an alumina source, a neutralizing agent, and a crystalline ZSM-5 nucleus to prepare a first solution in a solution state;mixing a second solution including a salt with the first solution to prepare a reaction mother liquor; andcontinuously supplying the reaction mother liquor to a hydrothermal synthesis reactor to perform continuous crystallization, {'br': None, 'i': W', '/W, 'sub': a', 'b, '0.2≤≤0.40\u2003\u2003[Equation 1]'}, 'wherein the following Equation 1 is satisfied{'sub': a', 'b, 'wherein Wis a content of the salt in the reaction mother liquor, and Wis a content of silica in the reaction mother liquor.'}2. The method for preparing ZSM-5-based zeolite of claim 1 , wherein a heating temperature is 30 to 60° C. and a heating time is 1 to 3 hours in the preparing of a first solution.3. The method for preparing ZSM-5-based zeolite of claim 1 , wherein the salt includes sodium sulfate (NaSO) claim 1 , sodium nitrate (NaNO) claim 1 , trisodium phosphate (NaPO) claim 1 , or a combination thereof.4. The method for preparing ZSM-5-based zeolite of claim 1 , wherein the hydrothermal synthesis reactor is a continuous stirred-tank reactor (CSTR) or a plug flow reactor (PFR).5. The method for preparing ZSM-5-based zeolite of claim 1 , wherein the second solution is an ...

METHOD FOR PRODUCING POLYCYCLIC AROMATIC COMPOUND SUBSTITUTED BY ARYL GROUP

PAH is subjected to C—H/C—B coupling using a specific boron compound, a palladium compound, and o-chloranil to produce a compound in which a C—H bond of the PAH is directly arylated regioselectively in a simple manner. When the substrate and the boron compound are appropriately selected, a larger PAH can also be obtained by further performing an annulation reaction after the coupling reaction. Similarly, when PAH is subjected to C—H/C—H cross-coupling using a specific aromatic compound, a palladium compound, and o-chloranil, a compound in which a C—H bond of the PAH is directly arylated regioselectively can be produced in a simple manner. When the substrate and the aromatic compound are appropriately selected in this case, a larger PAH can also be obtained by further performing an annulation reaction after the cross-coupling reaction. 1. A method for producing a polycyclic aromatic compound substituted with at least one substituted or unsubstituted aryl group , the method comprising reacting a polycyclic aromatic compound with a substituted or unsubstituted aryl-containing boron compound in the presence of a palladium compound and o-chloranil.2. The method according to claim 1 , wherein at least one hydrogen atom bonded to sphybridized carbon atoms of the polycyclic aromatic compound is replaced by a substituted or unsubstituted aryl group derived from the substituted or unsubstituted aryl-containing boron compound.5. The method according to claim 1 , wherein the palladium compound comprises zerovalent or divalent palladium.6. The method according to claim 1 , wherein the reaction of the polycyclic aromatic compound with the substituted or unsubstituted aryl-containing boron compound is performed in the presence of a silver compound.9. The method according to claim 7 , wherein step (II) is a step of performing an oxidation reaction using FeCl.10. A method for producing a polycyclic aromatic compound substituted with at least one substituted or unsubstituted aryl ...

PROCESS FOR THE ALKYLATION OF AROMATIC HYDROCARBONS WITH C1-C8 ALCOHOLS

Process for the alkylation of aromatic hydrocarbons by means of aliphatic alcohols containing from 1 to 8 carbon atoms, which comprises feeding the hydrocarbon and alcohol to the head of a fixed-bed reactor, operating with “trickle flow” regime, containing at least one layer of a catalyst comprising a zeolite selected from medium-pore zeolites and large-pore zeolites. 1. A process for the alkylation of aromatic hydrocarbons by means of aliphatic alcohols containing from 1 to 8 carbon atoms comprising: feeding the hydrocarbon and alcohol to the head of a fixed-bed reactor , operating under “trickle flow” regime , containing at least one layer of catalyst comprising a zeolite selected from medium-pore zeolites and large-pore zeolites.2. The process according to claim 1 , carried out in continuous claim 1 , which comprises:{'sub': 1', '8, 'a. mixing, in liquid phase, at least one aromatic hydrocarbon (A), a C-Calcohol (B) and a recycled stream (C) coming from a discharge section of the alkylation reactor,'}b. feeding the mixture obtained in step (a), pre-heated to the reaction temperature, to the head of a fixed-bed alkylation reactor, operating under “trickle flow” regime, containing at least one layer of catalyst comprising a zeolite selected from medium-pore zeolites and large-pore zeolites;c. cooling the reaction mixture in a discharge section, to obtain an organic phase, comprising the alkylated aromatic hydrocarbon and an aqueous phase essentially consisting of reaction water; andd. subdividing the organic phase into a recycled stream (C), sent to the head of the alkylation reactor for the mixing phase with the reagents, and a final stream, comprising the alkylated aromatic hydrocarbon.3. The continuous process according to claim 1 , which comprises:{'sub': 1', '8, 'a. mixing, in liquid phase, at least one aromatic hydrocarbon (A), and the C-Calcohol (B) with molar ratios A/B higher than 1;'}b. diluting the mixture coming from step (a) with a recycled stream ...

Catalysts for Selective Coupling of Olefins, and Methods of Making and Using Same

The present invention relates in part to the unexpected discovery of novel complexes capable of catalyzing the selective dehydrogenative coupling of olefins. The invention further relates to the use of these complexes for the selective coupling of olefins. 9. The method of claim 7 , wherein the olefin pressure ranges from about 0.1 atm to about 100 atm.10. The method of claim 7 , wherein the catalyst is contacted with the alkene at a temperature of about 100° C. to about 200° C.11. The method of claim 7 , wherein the olefin comprises ethylene.12. The method of claim 7 , wherein the conjugated 1 claim 7 ,3-diene comprises 1 claim 7 ,3-butadiene.13. The method of claim 7 , wherein the catalyst is in solution.14. The method of claim 13 , wherein the solution comprises at least one solvent selected from the group consisting of toluene claim 13 , benzene claim 13 , xylenes claim 13 , dioxane claim 13 , heptane claim 13 , pyridine claim 13 , tetrahydrofuran claim 13 , acetone claim 13 , acetonitrile claim 13 , butanol claim 13 , butanone claim 13 , carbon tetrachloride claim 13 , chlorobenzene claim 13 , chloroform claim 13 , cyclohexane claim 13 , dichloroethane claim 13 , diethylene glycol claim 13 , diethyl ether claim 13 , diglyme claim 13 , dimethyl formamide claim 13 , dimethyl sulfoxide claim 13 , ethanol claim 13 , ethyl acetate claim 13 , ethylene glycol claim 13 , glycerin claim 13 , hexamethylphosphoramide claim 13 , hexamethylphosphorous triamide claim 13 , hexanes claim 13 , methanol claim 13 , methylene chloride claim 13 , N-methyl-2-pyrrolidinone claim 13 , nitromethane claim 13 , pentane claim 13 , petroleum ether claim 13 , propanol and triethylamine.15. The method of claim 13 , wherein the solution further comprises at least one hydrogen acceptor additive. The present application claims priority under 35 U.S.C. § 119(e) to U.S. Provisional Patent Application No. 62/579,644, filed Oct. 31, 2017, which application is hereby incorporated by reference in its ...

Production of Para-Xylene

In a process for producing para-xylene, benzene and/or toluene is alkylated with methanol in the presence of a catalyst under conditions including a temperature of at least 500° C. and an HO partial pressure of at least 12 psia (83 kPaa). The catalyst comprises from 5 to 15 wt % ZSM-5, phosphorus or a compound thereof and a binder and has been steamed at a temperature of at least 900° C. The steamed catalyst has no more than two peaks in the P MAS NMR spectrum in the range of 0 to −50 ppm. 1. A process for producing para-xylene , the process comprising:{'sup': '−1', '(a) providing a catalyst comprising ZSM-5, phosphorus or a compound thereof and a binder, wherein the catalyst contains from 5 to 15 wt % ZSM-5 and has been steamed at a temperature of at least 900° C., wherein said steamed catalyst has a Diffusion Parameter for 2,2 dimethylbutane of about 0.1-15secwhen measured at a temperature of 120° C. and a 2,2 dimethylbutane pressure of 60 torr (8 kPa); and'}{'sub': '2', 'b': '12', '(b) alkylating benzene and/or toluene with an alkylating agent selected from methanol, dimethyl ether, and mixtures thereof, in the presence of said steamed catalyst under conditions including a temperature of at least 500° C. and an HO partial pressure of at least psia (83 kPaa).'}2. The process of claim 1 , wherein the catalyst in (a) comprises from 2 to less than 8 wt % of elemental phosphorus.35. The process of claim 1 , wherein the ZSM- is an aluminosilicate having a silica/alumina molar ratio of at least 200.4. The process of claim 1 , wherein the catalyst contains from 8 to 10 wt % ZSM-5.5. The process of claim 1 , wherein the binder comprises silica and/or clay.6. The process of claim 1 , wherein the catalyst contains from 75 to 90 wt % binder.7. The process of claim 1 , wherein the catalyst in (a) has been steamed at a temperature of at least 900° C. for between about 10 minutes and about 1.5 hours.8. The process claim 1 , wherein the conditions in (b) include an HO partial ...

PROCESS FOR THE PREPARATION OF BENZENE DERIVATIVES FROM FURAN DERIVATIVES

Benzene derivatives of the formula (I); 2. The process according to claim 1 , wherein Rand Rindependently comprise 1 to 8 carbon atoms claim 1 , optionally in addition to one or more oxygen atoms.3. The process according to claim 1 , wherein at least one of Rand Ris alkyl claim 1 , the alkyl group suitably comprising from 1 to 6 carbon atoms claim 1 , more preferably being methyl or ethyl.4. The process according to claim 1 , wherein at least one of Rand Ris a —COORgroup.5. The process according to claim 1 , wherein R claim 1 , R claim 1 , Rand Rindependently comprise from 1 to 7 claim 1 , preferably from 1 to 4 carbon atoms.6. The process according to claim 1 , wherein a desiccating agent is present.7. The process according to claim 6 , wherein the amount of desiccating agent is in the range of from 50 to 1000% wt claim 6 , based on the amount of furan derivative.8. The process according to claim 6 , wherein the desiccating agent is an organic desiccating agent.9. The process according to claim 8 , wherein the organic desiccating agent is a carboxylic acid anhydride.10. The process according to claim 9 , wherein the number of carbon atoms in the carboxylic acid anhydride ranges from 2 to 18 carbon atoms claim 9 , preferably from 2 to 8 carbon atoms.11. The process according to claim 9 , wherein the carboxylic acid anhydride is acetic anhydride claim 9 , benzoic anhydride or a mixture thereof.12. The process according to claim 1 , wherein further an additional dehydration catalyst is present.13. The process according to claim 12 , wherein the additional dehydration catalyst is a Diels Alder catalyst.14. The process according to claim 12 , wherein the additional dehydration catalyst has been selected from Lewis acids claim 12 , Brønsted acids claim 12 , activated carbon claim 12 , silica claim 12 , alumina claim 12 , silica-alumina claim 12 , zirconia claim 12 , zeolites and mixtures thereof.15. The process according to claim 12 , wherein the additional dehydration ...

METHODS OF PRODUCING PARA-XYLENE AND TEREPHTHALIC ACID

The present disclosure provides methods to produce para-xylene, toluene, and other compounds from renewable sources (e.g., cellulose, hemicellulose, starch, sugar) and ethylene in the presence of a catalyst. For example, cellulose and/or hemicellulose may be converted into 2,5-dimethylfuran (DMF), which may be converted into para-xylene by cycloaddition of ethylene to DMF. Para-xylene can then be oxidized to form terephthalic acid. 122-. (canceled)23. A method for producing para-xylene , comprising:a) combining 2,5-hexanedione with ethylene and a catalyst to form a reaction mixture, wherein the catalyst comprises a triflate; andb) producing para-xylene from at least a portion of the 2,5-hexanedione and at least a portion of the ethylene in the reaction mixture.24. The method of claim 23 , further comprising isolating the para-xylene from the reaction mixture.25. The method of claim 23 , wherein the catalyst is a metal triflate.26. The method of claim 23 , wherein the catalyst comprises a Group 3 metal cation claim 23 , a Group 9 metal cation claim 23 , a Group 10 metal cation claim 23 , a Group 11 metal cation claim 23 , or a lanthanide series metal cation.27. The method of claim 23 , wherein the catalyst comprises a divalent metal cation or a trivalent metal cation.28. The method of claim 23 , wherein the catalyst comprises Cu claim 23 , Co claim 23 , Cr claim 23 , Ni claim 23 , Mg claim 23 , Zn claim 23 , Al claim 23 , Bi claim 23 , Fe claim 23 , Gd claim 23 , In claim 23 , Nd claim 23 , La claim 23 , Sc claim 23 , or Y.29. The method of claim 23 , wherein the catalyst is bismuth triflate claim 23 , copper triflate claim 23 , cobalt triflate claim 23 , chromium triflate claim 23 , iron triflate claim 23 , cadmium triflate claim 23 , indium triflate claim 23 , nickel triflate claim 23 , manganese triflate claim 23 , tin triflate claim 23 , titanium triflate claim 23 , vanadium triflate claim 23 , yttrium triflate claim 23 , zinc triflate claim 23 , gadolinium ...

Conversion of Lignin to Fuels and Aromatics

Methods are provided for converting lignin-containing biomass into compounds that are more readily processed to form fuel and/or chemical products. The methods can allow for removal of at least a portion of the oxygen in lignin, either during or after depolymerization of lignin to single ring aromatic compounds, while optionally reducing or minimizing aromatic saturation performed on the aromatic compounds. The methods can include use of quench solvent to control reactions within the product stream from a pyrolysis process and/or use of a solvent to assist with hydroprocessing of lignin, lignin-containing biomass, or a pyrolysis oil. 1. A method of converting lignin to aromatic compounds , comprising:processing a lignin-containing feed under effective depolymerization conditions to form a depolymerized effluent containing monolignols;mixing the depolymerized effluent with a solvent to form a mixture of depolymerized effluent and solvent, the solvent having a T5 boiling point of at least about 240° C. and comprising at least about 50 wt % of aromatic compounds; andexposing at least a portion of the depolymerized effluent and solvent to a deoxygenation catalyst under effective deoxygenation conditions to form at least a deoxygenated effluent.2. The method of claim 1 , wherein processing a lignin-containing feed under effective depolymerization conditions comprises processing the lignin-containing feed under effective pyrolysis conditions in a pyrolysis reaction zone to form a pyrolysis effluent claim 1 , the pyrolysis effluent exiting the pyrolysis reaction zone at an exit temperature.3. The method of claim 2 , wherein mixing the depolymerized effluent with a solvent to form a mixture of depolymerized effluent and solvent comprises:mixing the pyrolysis effluent with a quench solvent, the quench solvent being at a quench solvent temperature and the pyrolysis effluent being at a mixing temperature that is less than about 100° C. different than the exit temperature; ...

PROCESS FOR PRODUCING PHENOL

In a process for producing phenol, benzene is contacted with a C3 alkylating agent comprising isopropanol under alkylation conditions such that at least part of the isopropanol reacts with the benzene to produce cumene. At least part of the resultant cumene is then oxidized in the presence of an oxidizing gas to produce an oxidation effluent comprising cumene hydroperoxide, unreacted cumene and a spent oxidizing gas. The unreacted cumene is separated from the oxidation effluent and is treated to remove nitrogenous impurities therefrom and produce a purified cumene stream, which is recycled to the oxidization step. At least part of the cumene hydroperoxide from the oxidation effluent is cleaved to produce a cleavage effluent comprising phenol and acetone. The phenol is recovered phenol from the cleavage effluent, whereas at least part of the acetone from the cleavage effluent is hydrogenated to produce isopropanol for recycle to the alkylation step. 1. A process for producing phenol , the process comprising:{'sub': '3', '(a) contacting benzene with a Calkylating agent comprising isopropanol, and optionally propylene, under alkylation conditions such that at least part of said isopropanol and benzene react to produce cumene;'}(b) oxidizing at least part of the cumene produced in (a) in the presence of an oxidizing gas to produce an oxidation effluent comprising cumene hydroperoxide and unreacted cumene and a spent oxidizing gas;(c) treating at least part of the unreacted cumene from the oxidation effluent to remove nitrogenous impurities therefrom and produce a purified cumene stream;(d) recycling the purified cumene stream to the oxidizing (b);(e) cleaving at least part of the cumene hydroperoxide from the oxidation effluent to produce a cleavage effluent comprising phenol and acetone;(f) recovering phenol from the cleavage effluent;(g) hydrogenating at least part of the acetone from the cleavage effluent to produce isopropanol; and(h) recycling at least part of the ...

AROMATIC ALKYLATION PROCESS

Processes and apparatuses for alkylating aromatic hydrocarbons with an alkylating reagent to produce an alkylated aromatic product are described. The processes and apparatuses use a riser reactor operated at a superficial velocity of 10 m/s to 25 m/s to produce the alkylated aromatic product. In some embodiments, a combination of steam and aromatic hydrocarbon is used to lift the catalyst. 1. A process for alkylating an aromatic hydrocarbon with an alkylating reagent to produce an alkylated aromatic product , comprising:{'sup': 3', '3, 'passing an aromatic hydrocarbon feed stream comprising an aromatic hydrocarbon and an alkylating reagent feed stream comprising an alkylating reagent to a riser reactor operated at a superficial velocity of 10 m/s to 25 m/s in the presence of a catalyst to produce a reaction mixture comprising the alkylated aromatic product, light olefins, and unreacted aromatic hydrocarbon, wherein the riser reactor comprises an operating catalyst density of about 325 kg/mto 600 kg/m; and'}recovering the alkylated aromatic product.2. The process of further comprising introducing one or more of steam or additional aromatic hydrocarbon into the riser reactor at a location in the riser reactor above where the aromatic hydrocarbon feed stream and the alkylating reagent feed stream are introduced.3. The process of claim 1 , wherein the riser reactor operates at a temperature of about 300° C. to about 700° C.4. The process of claim 1 , wherein the riser reactor operates at a pressure of about 68 kPa(g) to about 1378 kPa (g).5. The process of wherein the riser reactor has a residence time of about 0.5 seconds to about 6 seconds.6. (canceled)7. The process of wherein the aromatic hydrocarbon comprises toluene and the alkylating reagent comprises methanol claim 2 , and wherein a molar ratio of toluene to methanol is less than 4.8. The process of claim 1 , wherein a weight hourly space velocity of the riser reactor is about 10 hrto about 30 hr.9. The process ...

PROCESS TO MAKE OLEFINS AND AROMATICS FROM ORGANICS

The present invention relates to a process to make light olefins and aromatics, in a combined XTO-OC process, from an oxygen-containing, halogenide-containing or sulphur-containing organic feedstock comprising: 120-. (canceled)21. A process of making light olefins and aromatics , in a combined organics to olefins (XTO)-olefins conversion (OC) process , from an oxygen-containing , halogenide-containing or sulphur-containing organic feedstock 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 a first portion of an oxygen-containing, halogenide-containing, or sulphur-containing organic feedstock;providing an XTO reaction zone, an 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 sieve containing at least 10 membered rings pore opening in their microporous structure, wherein at least one of the catalysts comprises the catalyst composite;wherein each of the one or more catalysts circulates in the three zones, such that at least a portion of the regenerated one or more catalysts are passed to the OC reaction zone, at least a portion of the one or more catalysts in the OC reaction zone are passed to the XTO reaction zone and at least a portion of the one or more catalysts in the XTO reaction zone are passed to the regeneration zone;contacting the first portion of the oxygen-containing, halogenide-containing or sulphur-containing organic feedstock in the XTO reactor with the one or more catalysts at conditions effective to convert at least a portion of the feedstock to form a XTO reactor effluent comprising light olefins and a heavy hydrocarbon fraction;separating the light olefins from the ...

GROUP 8 TRANSITION METAL CATALYSTS AND METHOD FOR MAKING SAME AND PROCESS FOR USE OF SAME IN METATHESIS REACTION

Metal catalyst compounds are disclosed. The catalyst compound are represented by the formula (I-II and VII): wherein M is a Group 8 metal; X is an anionic ligand; L is a neutral two electron donor ligand; K 2 (A-E) is a ditopic or multitopic ligand. Also disclosed is an easy applicable catalyst synthesis and the application in different olefin metathesis processes, e.g. Reaction Injection Molding (RIM), rotational molding, vacuum infusion, vacuum forming, process for conversion of fatty acids and fatty acid esters or mixtures thereof, in -olefins, dicarboxylic acids or dicarboxylic esters, etc. 2. The catalysts according to claim 1 , wherein M is Ru or Os.3. The catalysts according to claim 1 , wherein Lis selected from phosphine claim 1 , sulphonated phosphine claim 1 , phosphate claim 1 , phosphinite claim 1 , phosphonite claim 1 , phosphite claim 1 , arsine claim 1 , stibine claim 1 , ether claim 1 , amine claim 1 , amide claim 1 , sulfoxide claim 1 , carboxyl claim 1 , nitrosyl claim 1 , pyridine claim 1 , substituted pyridine claim 1 , pyrazine claim 1 , thiocarbonyl claim 1 , thioether claim 1 , triazole carbene claim 1 , N-Heterocyclic carbene claim 1 , substituted NHC claim 1 , and a cyclic alkyl amino carbene.4. The catalysts according to claim 1 , wherein ligand Lrepresent a phosphine ligand having the formula P(Q)with Qare identical or different and are alkyl claim 1 , preferably C-Calkyl claim 1 , more preferably C-C-alkyl claim 1 , cycloalkyl- claim 1 , preferably C-Ccycloalkyl claim 1 , more preferably C-Ccycloalkyl claim 1 , preferably cyclopentyl claim 1 , cyclohexyl claim 1 , and neopentyl claim 1 , aryl claim 1 , preferably C-Caryl claim 1 , more preferably phenyl or toluyl claim 1 , alkyl-phosphabicyclononane claim 1 , C-Ccycloalkyl phospha-bicyclononane claim 1 , a sulfonated phosphine ligand of formula P(Q)wherein Qrepresents a mono- or poly-sulfonated Q-ligand; C-Caryl or C-C-alkyl-phosphinite ligand claim 1 , a C-Caryl or C-Calkyl phosphonite ...

General method for functionalizing carbon nanotubes via solvent free diels-alder reactions

The present invention provides methods by which carbon nanotubes can be functionalized via Diels-Alder reactions under solvent free conditions. Such methods include reacting carbon nanotubes with Diels-Alder dienes or dienophiles to obtain adducts that includes the diene or dienophile moiety bound to the carbon nanotubes. Functionalized carbon nanotubes and dispersions containing functionalized carbon nanotubes are provided. The present invention provides functionalization methods of carbon nanotubes through gas phase, liquid phase, or solid phase reactions without any solvents other than the reactants. Such processes are also amenable to a wide variety of chemical reactions that use other functionalizing agents. Additionally, such methods are cost effective, easily scalable and can provide for functionalized CNTs in large, industrial-scale quantities.

APPARATUSES FOR MIXING OF STAGED METHANOL INJECTION

This present disclosure relates to apparatuses for methylation of aromatics in an aromatics complex for producing a xylene isomer product. More specifically, the present disclosure relates to apparatuses for producing para-xylene by the selective methylation of toluene and/or benzene in an aromatics complex using processed toluene instead of crude toluene. 1. A riser reactor , comprising:a cylindrical riser comprising an outer wall and an inner wall;at least one baffle affixed to the inner wall extending into the riser; andat least one distributor configured to inject methanol into the riser, wherein the at least one distributor is located above the at least one baffle, below the at least one baffle, extends through the at least one baffle and into a different radial location within the riser reactor, or a combination thereof2. The riser reactor of claim 1 , wherein the at least one baffle extends around the entire inner wall of the riser reactor.3. The riser reactor of claim 1 , wherein the at least one distributor is angled from 30 degrees to 120 degrees relative to the inner wall.4. The riser reactor of claim 1 , further comprising a second distributor claim 1 , wherein the distributors are located at two different axial locations within the riser reactor.5. The riser reactor of claim 1 , wherein there are at least two rows of baffles.6. The riser reactor of claim 1 , further comprising a plurality of baffles and wherein the baffles are arranged symmetrically around the inner wall of the riser.7. The riser reactor of claim 1 , further comprising a plurality of baffles and wherein baffles cover substantially a circumference of the riser.8. The riser reactor of claim 1 , wherein the riser reactor is a toluene methylation riser reactor. This application is a continuation of U.S. Ser. No. 15/849,529 filed on Dec. 20, 2017, the entirety of which is incorporated herein by reference.This present disclosure relates to apparatuses for methylation of aromatics in an ...

APPARATUS AND PROCESS FOR CONVERTING AROMATIC COMPOUNDS BY BENZENE ALKYLATION WITH ETHANOL

Apparatus and process for converting aromatic compounds, comprising/using: a fractionating train (-) suitable for extracting at least one benzene-comprising fraction (), one toluene-comprising fraction () and one fraction () comprising xylenes and ethylbenzene from the feedstock (); a xylene separating unit () suitable for treating the fraction comprising xylenes and ethylbenzene and producing a para-xylene-comprising extract () and a raffinate () comprising ortho-xylene, meta-xylene and ethylbenzene; an isomerizing unit () for treating the raffinate and producing a para-xylene-enriched isomerizate (), which is sent to the fractionated train; and an alkylating reaction section () for treating at least part of the benzene-comprising fraction with an ethanol source () and producing an alkylation effluent () comprising ethylbenzene, which is sent to the isomerizing unit. 12. Apparatus for converting a feedstock () of aromatic compounds , comprising:{'b': 4', '7', '22', '23', '24', '2, 'a fractionating train (-) suitable for extracting at least one fraction comprising benzene (), one fraction comprising toluene () and one fraction comprising xylenes and ethylbenzene () from the feedstock ();'}{'b': 10', '24', '39', '40, 'a xylene separating unit () suitable for treating the fraction comprising xylenes and ethylbenzene () and for producing an extract () comprising para-xylene and a raffinate () comprising ortho-xylene, meta-xylene and ethylbenzene;'}{'b': 11', '40', '42', '4', '7, 'an isomerizing unit () suitable for treating the raffinate () and producing a para-xylene-enriched isomerizate (), which is sent to the fractionating train (-); and'}{'b': 13', '22', '30', '31', '11, 'an alkylating reaction section () suitable for treating at least part of the fraction comprising benzene () with an ethanol source () and producing an alkylating effluent () comprising ethylbenzene, which is sent to the isomerizing unit ().'}214313247. Conversion apparatus according to claim 1 , ...