СПОСОБ ОБРАБОТКИ ПОЛИАЛКИЛАРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ

Настоящее изобретение относится к способу обработки полиалкилароматических углеводородов. В представленном способе обработки смеси, содержащей полиалкилированные ароматические соединения, проводят восстановление водородом полиароматических соединений в присутствии катализатора гидрирования кислородсодержащих органических субстратов. Указанные полиароматические соединения получают в процессе алкилирования ароматических соединений с помощью алкилирующего агента, выбираемого из спиртов, первичных олефинов или их смесей. При этом количество ароматических колец, которые подвергаются гидрированию в процессе востановления водородом, составляет меньше 1% относительно всех ароматических колец. Предложенный в изобретении подход позволяет увеличить стабильность и продолжительность работы катализатора транс-алкилирования. 2 н. и 20 з.п. ф-лы, 3 табл., 3 пр.

ТЕПЛОВАЯ ИНТЕГРАЦИЯ В ПРОЦЕССАХ ДИСПРОПОРЦИОНИРОВАНИЯ ИЛИ ПЕРЕАЛКИЛИРОВАНИЯ

Изобретение относится к двум вариантам способа переалкилирования и установке. При этом один из вариантов способа предусматривает стадии: (a) проведения в реакторе реакции потока сырья реактора, содержащего толуол, С9-ароматические вещества, С10-ароматические вещества и водород, на катализаторе для получения выходящего потока реактора, содержащего бензол и ксилолы; (b) охлаждения выходящего потока реактора с получением первой двухфазной смеси; (c) разделения первой двухфазной смеси на первый жидкий поток и первый парообразный поток; (d) подачи, по меньшей мере, части первого жидкого потока в колонну получения бензола, причем часть первого жидкого потока, подаваемого в колонну получения бензола, обходит стабилизационную колонну; и (e) извлечения бензола из первого сконденсированного жидкого потока в колонне получения бензола. Предложенное изобретение позволяет повысить энергоэффективность процессов. 3 н. и 28 з.п. ф-лы, 3 табл., 8 пр., 4 ил.

СПОСОБ ПРЕОБРАЗОВАНИЯ СМЕСЕЙ, СОДЕРЖАЩИХ АРОМАТИЧЕСКИЕ УГЛЕВОДОРОДЫ CВ ИЗОМЕРЫ КСИЛОЛА

... 1. Способ получения изомеров ксилола, включающий:(a) контактирование сырья, содержащего ароматические соединения С, с катализатором в условиях, необходимых для превращения сырья в поток промежуточных продуктов, содержащих изомеры ксилола;(b) выделение по меньшей мере части изомеров ксилола из потока промежуточных продуктов и(c) возвращение в сырье стадии (а) потока промежуточных продуктов, обедненных изомерами ксилола, полученного на стадии (b).2. Способ по п.1, в котором сырье практически не содержит изомеров ксилола, серы, парафинов и олефинов.3. Способ по п.1, в котором сырье содержит меньше примерно 50 масс.% толуола в расчете на общую массу сырья.4. Способ по п.1, в котором сырье содержит меньше примерно 30 масс.% бензола в расчете на общую массу сырья.5. Способ по п.1, в котором катализатор представляет собой несульфидированный широкопористый цеолит, пропитанный оксидом металла VIB группы.6. Способ по п.5, в котором цеолит выбирают из группы, состоящей из морденита, цеолита бета и ...

СПОСОБ ПРИГОТОВЛЕНИЯ КАТАЛИЗАТОРА И СПОСОБ ПОЛУЧЕНИЯ ИЗОПРОПИЛБЕНЗОЛА С ИСПОЛЬЗОВАНИЕМ ЭТОГО КАТАЛИЗАТОРА

Изобретение относится к способу получения изопропилбензола в процессе алкилирования бензола пропиленом при температуре 170-230°C, давлении от атмосферного до 50 атм, мольном отношении бензол/пропилен в исходной смеси от 4:1 до 10:1, весовой скорости подачи исходной смеси от 0,2 до 10 ч-1с использованием катализатора на основе цеолита Бета, приготовленного контактированием цеолита Бета с раствором нитрата аммония для удаления соединений натрия и переведения цеолита в водородную форму, с последующими стадиями грануляции со связующим, сушки и прокаливания гранул, причем цеолит Бета перед грануляцией со связующим предварительно подвергают обработке раствором хелатирующего агента, а затем обрабатывают перегретым водяным паром при температуре не выше 550°С в течение не менее 2 ч, в качестве хелатирующиего агента применяют сульфосалициловую кислоту, этилендиаминтетрауксусную кислоту ЭДТА, сульфобензойную кислоту, 3-гидроксинафталин-1,4-дисульфокислоту. Технический результат заключается в увеличении ...

КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ, ЕЕ ПОЛУЧЕНИЕ И СПОСОБ ПРИМЕНЕНИЯ УКАЗАННОЙ КОМПОЗИЦИИ

СПОСОБ ПОЛУЧЕНИЯ ИЗОПРОПИЛБЕНЗОЛА

Selektive Herstellung von 2,6-Diäthylnaphthalin.

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

HYDROCARBON CONVERSION

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

PROCEDURE FOR THE TRANSFORMATION OF HIGH-SIMMERING AROMATICS

PROCEDURE FOR THE PRODUCTION OF SECOND BUTYLBENZOL

PROCEDURE FOR THE CATALYTIC DISPROPORTIONATION OF METHYLNAPHTHALENEN.

IN SITU DECREASE OF THE COKING OF A POROUS CATALYST IN A SUPERCRITICAL REACTION MEDIUM

METHOD FOR PRODUCING M-BENZYLTOLUENE

A method for producing m-benzyltoluene with a high yield and excellent selectivity without producing undesirable heavier by-products. The method is characterized in that toluene and diphenylmethane are allowed to react at a reaction temperature in the range of 170 to 400.degree.C in the presence of a crystalline synthetic zeolite catalyst in which the molar ratio of SiO2/Al2O3 is 20 or higher and the openings of main pores are formed by ten-membered oxygen rings.

PROCESS FOR THE TRANSALKYLATION OR DEALKYLATION OF ALKYL AROMATIC HYDROCARBONS

TRANSALKYLATION PROCESS AND CATALYST COMPOSITION USED THEREIN

The present disclosure relates to a process for producing a mono-alkylated aromatic compound, such as, for example, ethylbenzene or cumene, in which an alkylatable aromatic compound stream, such as, for example, benzene, and an alkylation agent stream, such as, for example, poly-ethylbenzene or poly-isopropylbenzene, are contacted in the presence of a trans alkylation catalyst and under at least partial liquid phase transalkylation conditions. The trans alkylation catalyst comprises a zeolite having a framework structure selected from the group consisting of FAU, BEA*, MOR, MWW and mixtures thereof. The zeolite has a silica- alumina molar ratio in a range of 10 to 15. The transalkylation catalyst composition has an external surface area/volume ratio in the range of 30 cm 1 to 85 cm 1.

Verfahren zur Ausführung von intra- und/oder intermolekularen Umlagerungen von alkylsubstituierten aromatischen Kohlenwasserstoffen

Transalkylation of heavy aromatic hydrocarbon feedstocks

In a process for producing xylene by transalkylation of a C9+ aromatic hydrocarbon feedstock with a C6 and/or C7 aromatic hydrocarbon, the C9+ aromatic hydrocarbon feedstock, at least one C6 and/or C7 aromatic hydrocarbon and hydrogen are contacted with a first catalyst comprising (i) a first molecular sieve having a Constraint Index in the range of about 3 to about 12 and (ii) at least first and second different metals or compounds thereof of Groups 6 to 12 of the Periodic Table of the Elements. Contacting with the first catalyst is conducted under conditions effective to dealkylate aromatic hydrocarbons in the feedstock containing C2+ alkyl groups and to saturate C2+ olefins formed so as to produce a first effluent. At least a portion of the first effluent is then contacted with a second catalyst comprising a second molecular sieve having a Constraint Index less than 3 under conditions effective to transalkylate C9+ aromatic hydrocarbons with said at least one C6-C7 aromatic hydrocarbon ...

Conversion of aromatic hydrocarbons

A process for the transalkylation of an aromatic feedstock containing a benzene component and a polyalkylated aromatic component comprising at least one polyalkyl aromatic compound of at least nine carbon atoms. The feedstock is supplied to a reaction zone containing a metal modified zeolite transalkylation catalyst. The reaction zone is operated under conditions providing an equivalent conversion of pure toluene in the presence of the catalyst within the range of 40-55%, resulting in a transalkylated product with a reduced polyalkyl benzene content and an enhance monoalkyl benzene content relative to the transalkylation feedstock. In continued operation of the transalkylation reaction zone, at least one of the reaction conditions of temperature, pressure, and space velocity is adjusted in order to maintain a constant reaction severity to provide a desired equivalent conversion of toluene within a tolerance range of 2%. Specifically, the temperature is progressively increased while continuing ...

METHOD FOR PRODUCING MONOCYLIC AROMATIC HYDROCARBONS

This method for producing monocyclic aromatic hydrocarbons involves producing monocylic aromatic hydrocarbons with 6 to 8 carbon atoms, and comprises: a decomposition reforming reaction step in which oil feedstock is brought into contact with a catalyst to produce a reaction, thereby obtaining a product containing monocyclic aromatic hydrocarbons with 6 to 8 carbon atoms, and a heavy distillate with 9 or more carbon atoms; a purification and recovery step for purifying and recovering the monocyclic aromatic hydrocarbons with 6 to 8 carbon atoms, which were separated from the product generated in the decomposition reforming reaction step; and a first return step for returning at least some of the toluene obtained in the purification and recovery step to the decomposition reforming reaction step.

Aromatics and toluene/trimethylbenzene gas phase transalkylation processes

A gas phase, aromatics transalkylation process that comprises contacting a stream containing aromatic hydrocarbons with a catalyst comprising a zeolite selected from the group consisting of SSZ-26, Al-SSZ-33, CIT-1, SSZ-35, and SSZ-44 in the presence of added hydrogen and in the gas phase, to produce transalkylated product. The aromatics stream comprises one or more aromatic hydrocarbons, one of the hydrocarbons having at least one alkyl group attached thereto, the alkyl group comprising a C1, C2, C3 or C4 hydrocarbyl group. A preferred aromatics transalkylation process comprises contacting toluene or benzene or a mixture thereof with a stream containing trimethylbenzene in the presence of added hydrogen. The catalyst preferably contains a mild hydrogenation metal, such as nickel or palladium.

Synthesis of ZSM-12

This invention provides a process for the synthesis of ZSM-12 using the N,N-dimethylhexamethyleneimine cation as a directing agent. The process enables ZSM-12 to be produced at silica/alumina molar ratios below 50 with little or no co-production of impurity phases. Small crystal forms of ZSM-12 can also be produced using the process of the invention.

TREATING C8-C10 AROMATIC FEED STREAMS TO PREPARE AND RECOVER TRIMETHYLATED BENZENES

Methods are provided for the treatment of a feed stream containing C9 aromatic components to produce mesitylene-containing products. The methods include hydrodealkylating the feed stream to remove C2 and higher alkyl groups from the aromatic components and transalkylating the feed stream to rearrange the distribution of methyl groups among the aromatic components. Disclosed methods also include the treatment of a hydrocarbon feedstock by hydrodealkylation and/or transalkylation in order to produce a hydrocarbon product having an increased mass percentage of mesitylene.

СПОСОБ ПОЛУЧЕНИЯ ИЗОПРОПИЛБЕНЗОЛА

Изобретение относится к способу получения изопропилбензола алкилированием бензола пропиленом и переалкилированием полиалкилибензолов. Способ характеризуется тем, что реакции алкилирования и переалкилирования проводят раздельно, причем реакцию алкилирования проводят в жидкой фазе с применением полимерного катализатора, имеющего только Бренстодовые кислотные центры, а для осуществления реакции переалкилирования в качестве катализатора применяют кислоту Льюиса. Использование предлагаемого способа позволяет повысить эффективность процесса посредством использования оптимального температурного режима. 4 з.п. ф-лы, 3 пр., 1 ил.

СЕНСОР, КОТОРЫЙ ВВОДИТ ПОПРАВКУ НА ДЕГРАДАЦИЮ ЛЮМИНЕСЦИРУЮЩЕЙ СРЕДЫ

Изобретение относится к сенсору (12), который генерирует выходной сигнал под действием возбуждающего сигнала. В устройстве выходной сигнал генерируется с заранее установленной зависимостью от одного или более свойств возбуждающего сигнала, так что одно или более свойства возбуждающего сигнала могут определяться как функция выходного сигнала. В одном варианте осуществления сенсор содержит компонент (24), процессор сенсора (26) и трансмиттер (28). Компонент деградирует, вызывая тем самым прогнозируемые отклонения от заранее установленной зависимости между выходным сигналом и одним или более свойствами возбуждающего сигнала. Процессор сенсора предоставляет информацию о деградации компонента. Трансмиттер по беспроводной линии связи передает эту информацию, предоставленную процессором. 3 н. и 24 з.п. ф-лы, 5 ил.

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 ...

КРИСТАЛЛИЧЕСКИЕ ГЕРМАНОСИЛИКАТНЫЕ МАТЕРИАЛЫ НОВОЙ ТОПОЛОГИИ CIT-13 И СПОСОБЫ ИХ ПОЛУЧЕНИЯ

Изобретение относится к новым кристаллическим германосиликатным композициям и способам их получения. Кристаллические германосиликатные композиции, пригодные в катализе и для разделения газов, представляют собой композиции, содержащие трехмерный каркас, имеющий поры, определяемые 10- и 14-членными кольцами. Изобретение описывает способы получения данных композиций с использованием замещенных бензилимидазолиевых органических структурообразующих агентов (ОСОА). Также раскрыты способы применения данных кристаллических композиций. Обеспечиваются композиции с увеличенными размерами пор, способные обрабатывать более крупные молекулы. 7 н. и 30 з.п. ф-лы, 37 ил., 15 табл., 25 пр.

ТЕПЛОВАЯ ИНТЕГРАЦИЯ В ПРОЦЕССАХ ДИСПРОПОРЦИОНИРОВАНИЯ ИЛИ ПЕРЕАЛКИЛИРОВАНИЯ

СПОСОБ ПРОИЗВОДСТВА КСИЛОЛОВ И ФЕНОЛА ИЗ ПОЛУЧЕННЫХ ИЗ УГЛЯ ЖИДКОСТЕЙ

СПОСОБ ПОЛУЧЕНИЯ МОЛЕКУЛЯРНОГО СИТА

СЕНСОР, КОТОРЫЙ ВВОДИТ ПОПРАВКУ НА ДЕГРАДАЦИЮ ЛЮМИНЕСЦИРУЮЩЕЙ СРЕДЫ

... 1. Сенсор (12) сконфигурирован для получения информации, относящейся к одному или более газовым аналитам в объеме газа, сенсор содержит ! (а) первую секцию сенсора (16), которая содержит эмиттер (30), эмиттер сконфигурирован на испускание электромагнитного излучения; и ! (b) вторую секцию сенсора (18), сконфигурированную соединяться с первой секцией сенсора с возможностью съема, вторая секция сенсора содержит ! (1) люминесцирующую среду (24), действующим образом взаимодействующую с объемом газа и расположенную для приема электромагнитного излучения от эмиттера, если вторая секция сенсора соединена с первой секцией сенсора с возможностью съема, где люминесцирующая среда испускает люминесцентное излучение в ответ на электромагнитное излучение, которое она получает от эмиттера, причем информация, относящаяся к одному или более газовым аналитам в объеме газа, может быть определена как функция одного или более свойств люминесцентного излучения, ! (2) модуль памяти (26, 50), который хранит информацию ...

СПОСОБ ТРАНСАЛКИЛИРОВАНИЯ И ПРИМЕНЯЮЩАЯСЯ В НЕМ КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ

Isomerization and disproportionation of aromatic hydrocarbons

PROCEDURE FOR THE PRODUCTION OF 2,6 - DIMETHYLNAPHTHALIN

Methods of making xylene isomers

ISOMERISATION OF ALKYL AROMATICS USING A GALLIUM CONTAINING ALUMINOSILICATE CATALYST

The present invention relates to a process for the hydrocatalytic treatment of a hydrocarbon feedstock which is a mixture of alkyl aromatics containing at least one di- or polymethyl benzene and an alkyl benzene selected from ethyl-benzene, methyl ethyl-benzene and propylbenzene by contacting the mixture at 300.degree. to 500.degree.C, a pressure of 0 to 100 bars gauge and in the presence of hydrogen with a gallium containing aluminosilicate catalyst and recovering the desired product. The aluminosilicate has a silica to alumina ratio of between 10:1 and 100:1 on a molar bases. The xylene products are useful raw materials as such or for making the corresponding dicarboxylic acids.

HYDROCARBON CONVERSION

ISOMERISED PRODUCTION PROCESSING UNIT COM AND TRANSALKYLATION OF XYLENE

Method for producing light aromatic producing high-value light aromatics by using heavy aromatics that are difficult to treat and utilize

A method for producing a light aromatic comprises: i) bringing a raw material containing a heavy aromatic into contact with a catalyst in a fluidized reactor, and carrying out an aromatic lightening reaction under hydrogen conditions to obtain products rich in C6-C8 light aromatics and a spent catalyst, wherein the heavy aromatic is selected from one or more of C9+ aromatics; ii) separating the products rich in C6-C8 light aromatics to obtain hydrogen, non-aromatic components, C6-C8 light aromatics, and C9+ aromatic components; and iii) returning at least part of the C9+ aromatic components to the fluidized reactor. The method has strong adaptability to raw materials, flexible operation, and high flexibility, and can ensure long-term stable operation. The method can produce high-value light aromatics by using heavy aromatics that are difficult to treat and utilize.

TRANSALKYLATION OF HEAVY AROMATIC HYDROCARBON FEEDSTOCKS

In a process for producing xylene by transalkylation of a C9+ aromatic hydrocarbon feedstock with a C6 and/or C7 aromatic hydrocarbon, the C9+ aromatic hydrocarbon feedstock, at least one C6 and/or C7 aromatic hydrocarbon and hydrogen are contacted with a first catalyst comprising (i) a first molecular sieve having a Constraint Index in the range of about 3 to about 12 and (ii) at least first and second different metals or compounds thereof of Groups 6 to 12 of the Periodic Table of the Elements. Contacting with the first catalyst is conducted under conditions effective to dealkylate aromatic hydrocarbons in the feedstock containing C2+ alkyl groups and to saturate C2+ olefins formed so as to produce a first effluent. At least a portion of the first effluent is then contacted with a second catalyst comprising a second molecular sieve having a Constraint Index less than 3 under conditions effective to transalkylate C9+ aromatic hydrocarbons with said at least one C6-C7 aromatic hydrocarbon ...

A process of using a high activity catalyst for the transalkylation of aromatics

Conversion of aromatic hydrocarbons

$i(IN SITU) MITIGATION OF COKE BUILD-UP IN POROUS CATALYSTS BY PRETREATMENT OF HYDROCARBON FEED TO REDUCE PEROXIDES AND OXYGEN IMPURITIES

A process is provided for in situ mitigation of coke build-up in porous catalyst used for the processing of hydrocarbon feed stocks. The feed is continuously maintained deoxygenated in reactor unit (10) by bubbling helium fed via line (14) to bottle (12) and through the hexene feed such that the head space (16) is always blanked with helium. The 1-hexene feed is pumped from bottle (12) through line (18) to the suction of HPLC pump (20), and thereafter through line (22) to peroxide trap (24). Peroxide trap (24) is a stainless steel tube packed with alumina.

КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ, ЕЕ ПОЛУЧЕНИЕ И СПОСОБ ПРИМЕНЕНИЯ УКАЗАННОЙ КОМПОЗИЦИИ

Изобретение относится к каталитической композиции для трансалкилирования исходного сырья, содержащего ароматические углеводороды, которая содержит носитель и один или более металлических компонентов, нанесенных на носитель, причем указанный носитель содержит (i) морденит в количестве от 30 до 70% мас. в расчете на общую массу носителя, и морденит имеет молярное отношение диоксида кремния к оксиду алюминия от 15 до 60; (ii) цеолит типа ZSM-5 в количестве от 15 до 60% мас. в расчете на общую массу носителя, и цеолит типа ZSM-5 имеет молярное отношение диоксида кремния к оксиду алюминия от 5 до 50 и средний размер частиц от 5 до 50 нм; и (iii) неорганическое связующее вещество в количестве от 10 до 40% мас. в расчете на общую массу носителя; и при этом один или более металлических компонентов содержат металл 10 группы. Также изобретение относится к способу получения заявленной каталитической композиции и к способу трансалкилирования исходного сырья, содержащего ароматические углеводороды, ...

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА НА ОСНОВЕ МОЛИБДЕНА И ПЛАТИНЫ ДЛЯ СИНТЕЗА БЕНЗОЛА ПУТЕМ ТРАНСАЛКИЛИРОВАНИЯ

УСТРОЙСТВА И СПОСОБЫ ДЛЯ РАЗДЕЛЕНИЯ ИЗОМЕРОВ КСИЛОЛА С ИСПОЛЬЗОВАНИЕМ СЕЛЕКТИВНОЙ АДСОРБЦИИ

Verfahren zur Alkylierung,Umalkylierung und Isomerisierung von Kohlenwasserstoffen

CRYSTALLINE GALLOSILICATES

CONVERSION OF AROMATIC HYDROCARBONS

PROCEDURE FOR THE CONVERSION OF AROMATIC HYDROCARBONS

Aromatics and toluene/trimethylbenzene gas phase transalkylation processes

Alkylated aromatic compounds

CONVERSION METHOD OF HEAVY AROMATICS

PURPOSE: A method for converting heavy aromatics and a converted product obtained by the method are provided, to convert the heavy aromatics comprising a C8+ alkyl aromatic compound into benzene, toluene or xylene. CONSTITUTION: The method comprises the steps of providing a reaction region containing a mordenite catalyst; introducing source materials into the reaction region to allow the source materials to be contact with the mordenite catalyst under the selected condition; converting the source materials under the initially selected condition; controlling the reactor condition needed to maintaining the conversion of source materials; and removing the converted product from the reaction region. Preferably the mordenite catalyst is selected from a nickel-containing mordenite catalyst, a palladium-containing mordenite catalyst or a platinum-containing mordenite catalyst. © KIPO 2003 ...

processo e unidade de processo de isomerização e transalquilação de xileno combinadas

Y-85 and modified LZ-210 zeolites

Catalysts for converting polyalkylaromatics to monoalkylaromatics, particularly cumene and ethyl benzene are disclosed which comprise aY-85 or a modified LZ-210 zeolite. For cumene and ethylbenzene production, a disclosed catalyst, made of 80 wt% zeolite and 20 wt% alumina binder on a volatile-free basis, has one or more of the following physical characteristics: (1) an absolute intensity of the Y-85 or modified LZ-210 zeolite as measured by X-ray diffraction (XRD) of preferably at least 50 and (2) a framework aluminum of the Y-85 or modified LZ-210 zeolite of preferably at least 60% of the aluminum of the Y-85 or modified LZ-210 zeolite.

CATALYST COMPOSITION, ITS PREPARATION AND PROCESS USING SUCH COMPOSITION

Catalyst composition comprising a carrier and one or more Group 10 metal components, wherein the carrier comprises (i) 20 to 90 wt % mordenite having a silica to alumina molar ratio in the range of from 10 to 60; (ii) 10 to 70 wt % ZSM-5 type zeolite having a silica to alumina molar ratio in the range of from 5 to 50 and an average particle size in the range of from 5 to 50 nm; and (iii) 10 to 50 wt % of binder; a process for preparing the catalyst, and a process for the conversion of an aromatic hydrocabons-containing feedstock using the catalyst. 1. A catalyst composition which comprises a carrier and one or more metal components supported on the carrier , wherein the carrier comprises (i) mordenite in an amount in the range of from 20 to 90 wt % , based on total weight of carrier , the mordenite having a silica to alumina molar ratio in the range of from 10 to 60; (ii) ZSM-5 type zeolite in an amount of from 10 to 70 wt % , based on total weight of carrier , the ZSM-5 type zeolite having a silica to alumina molar ratio in the range of from 5 to 50 and an average particle size in the range of from 5 to 50 nm; and (iii) an inorganic binder in an amount in the range of from 10 to 50 wt % , based on total weight of carrier; and wherein the one or more metal components comprise a group 10 metal.2. The catalyst composition according to claim 1 , wherein the mordenite is present in an amount in the range of from 30 to 70 wt % claim 1 , based on total weight of carrier.3. The catalyst composition according to claim 1 , wherein the ZSM-5 type zeolite is present in an amount in the range of from 15 to 60 wt % claim 1 , based on total weight of carrier.4. The catalyst composition according to claim 1 , wherein the inorganic binder is present in an amount in the range of from 10 to 40 wt % claim 1 , based on total weight of carrier material.5. The catalyst composition according to claim 1 , wherein the ZSM-5 type zeolite has a number average particle size in the range of ...

Energy efficient fractionation process for separating the reactor effluent from TOL/A9+ transalkylation processes

Processes and apparatus are disclosed for the energy efficient separation of the effluent from a TOL/A9+ transalkylation reactor. The apparatus includes a reboiled prefractionation column and a sidedraw tower that produces: 1) an overhead stream including unreacted toluene, 2) a stream including unreacted C9+ aromatics, a portion of which stream may be recycled to the reactor; and 3) a sidedraw stream including C8 aromatics that may be directed to a crystallization or selective adsorption paraxylene separation unit for recovery o a paraxylene product.

Рrосеss fоr prоduсing phеnоl аnd mеthуl еthуl kеtоnе

А prосеss fоr prоduсing sес-butуlbеnzеnе соmprisеs соntасting а fееd соmprising bеnzеnе аnd а С4 аlkуlаting аgеnt undеr аlkуlаtiоn соnditiоns соmprising а tеmpеrаturе оf аbоut 110° С. tо аbоut 150° С. with а саtаlуst соmprising аt lеаst оnе mоlесulаr siеvе hаving аn Х-rау diffrасtiоn pаttеrn inсluding d-spасing mахimа аt 12.4±0.25, 6.9±0.15, 3.57±0.07 аnd 3.42±0.07 Аngstrоm. Тhе sес-butуlbеnzеnе саn bе thеn охidizеd tо prоduсе а hуdrоpеrохidе аnd thе hуdrоpеrохidе dесоmpоsеd tо prоduсе phеnоl аnd mеthуl еthуl kеtоnе.

Рrосеss fоr prоduсing phеnоl аnd mеthуl еthуl kеtоnе

А prосеss fоr prоduсing sес-butуlbеnzеnе соmprisеs соntасting а fееd соmprising bеnzеnе аnd а С4 аlkуlаting аgеnt undеr аlkуlаtiоn соnditiоns соmprising а tеmpеrаturе оf аbоut 110° С. tо аbоut 150° С. with а саtаlуst соmprising аt lеаst оnе mоlесulаr siеvе hаving аn Х-rау diffrасtiоn pаttеrn inсluding d-spасing mахimа аt 12.4±0.25, 6.9±0.15, 3.57±0.07 аnd 3.42±0.07 Аngstrоm. Тhе sес-butуlbеnzеnе саn bе thеn охidizеd tо prоduсе а hуdrоpеrохidе аnd thе hуdrоpеrохidе dесоmpоsеd tо prоduсе phеnоl аnd mеthуl еthуl kеtоnе.

Рrосеss fоr prоduсing phеnоl аnd mеthуl еthуl kеtоnе

А prосеss fоr prоduсing sес-butуlbеnzеnе соmprisеs соntасting а fееd соmprising bеnzеnе аnd а С4 аlkуlаting аgеnt undеr аlkуlаtiоn соnditiоns соmprising а tеmpеrаturе оf аbоut 110° С. tо аbоut 150° С. with а саtаlуst соmprising аt lеаst оnе mоlесulаr siеvе hаving аn Х-rау diffrасtiоn pаttеrn inсluding d-spасing mахimа аt 12.4±0.25, 6.9±0.15, 3.57±0.07 аnd 3.42±0.07 Аngstrоm. Тhе sес-butуlbеnzеnе саn bе thеn охidizеd tо prоduсе а hуdrоpеrохidе аnd thе hуdrоpеrохidе dесоmpоsеd tо prоduсе phеnоl аnd mеthуl еthуl kеtоnе.

Рrосеss fоr prоduсing phеnоl аnd mеthуl еthуl kеtоnе

А prосеss fоr prоduсing sес-butуlbеnzеnе соmprisеs соntасting а fееd соmprising bеnzеnе аnd а С4 аlkуlаting аgеnt undеr аlkуlаtiоn соnditiоns соmprising а tеmpеrаturе оf аbоut 110° С. tо аbоut 150° С. with а саtаlуst соmprising аt lеаst оnе mоlесulаr siеvе hаving аn Х-rау diffrасtiоn pаttеrn inсluding d-spасing mахimа аt 12.4±0.25, 6.9±0.15, 3.57±0.07 аnd 3.42±0.07 Аngstrоm. Тhе sес-butуlbеnzеnе саn bе thеn охidizеd tо prоduсе а hуdrоpеrохidе аnd thе hуdrоpеrохidе dесоmpоsеd tо prоduсе phеnоl аnd mеthуl еthуl kеtоnе.

СПОСОБ ПОЛУЧЕНИЯ ИЗОМЕРОВ КСИЛОЛА (ВАРИАНТЫ)

Изобретение относится к способу получения изомеров ксилола. Способ включает контактирование сырья, содержащего ароматические углеводороды С, на несульфидированном катализаторе, имеющем объем макропор от приблизительно 0,02 см/г до приблизительно 0,5 см/г. При этом катализатор включает носитель, импрегнированный компонентом гидрирования, представляющим собой металл VIB группы или его оксид, носитель включает макропористое связующее с размерами пор более 500 ангстрем и крупнопористое сито с размерами пор по крайней мере 6 ангстрем, при среднечасовой скорости подачи сырья от 0,1 до 30, давлении от 0,17 до 6,9 МПа и более, температуре от 200 до 800°С. Также изобретение относится к способу получения изомеров ксилола, включающему контактирование сырья, содержащего ароматические углеводороды С-C, использующему аналогичный катализатор. Использование предлагаемого изобретения позволяет снять диффузионные ограничения, наблюдаемые при использовании высокоактивных катализаторов с недостатком таких ...

Способ получения изопропилбензола трансалкилированием диизопропилбензолов с бензолом

Изобретение относится к способу получения изопропилбензола трансалкилированием диизопропилбензолов с бензолом. Способ включает проведение процесса трансалкилирования в однополочном контактном трансалкилаторе с адиабатическим слоем цеолитсодержащего катализатора, последующую ректификацию продуктов реакции трансалкилирования и выделение рециклового бензола, изопропилбензола, диизопропилбензолов и тяжелых полиалкилбензолов. Способ характеризуется тем, что процесс трансалкилирования диизопропилбензолов с бензолом проводят при температуре 190÷230°С, давлении 2,0÷3,0 МПа, мольном отношении бензол/диизопропилбензолы 2:1÷6:1, объемной скорости подачи сырья 1÷5 ч-1, объемной скорости по диизопропилбензолам 0,3÷1,3 ч-1 в присутствии гетерогенного цеолитсодержащего катализатора, содержащего, мас.%: оксид церия 0,4-0,6, цеолит USY в NH3-форме с мольным отношением SiO2/Al2O3 = 11 49,7-49,8, связующее γ-Al2O3 - остальное. Изобретение обеспечивает повышение каталитической активности катализатора, что ...

СПОСОБ ПОЛУЧЕНИЯ 2,6-ДИЭТИЛНАФТАЛИНА

Использование: в нефтехимии, в частности в производстве нафталиндикарбоновых кислот-мономеров для синтеза, например полиэтилен-2,6-нафталатов. Сущность изобретения: продукт - смесь 2,6- и 2,7-диэтилнафталинов. Реагент 1: нафталин и/или 2-этилнафталин. Реагент 2: этилирующий агент - 1,2,4-триэтилбензол, тетраэтилбензолы (преимущественно смесь изомеров) и/или пентаэтилбензол. Условия реакции: в присутствии катализатора - кислоты Льюиса: AlCl3, AlBr3, SbF5 , TaCl5 или комплекс AlCl3 с хлористым или бромистым этилом (предпочтительно AlCl3 или указанный комплекс), при молярном соотношении реагентов 1 и 2 1 : (1 - 10), лучше 1 : (2 - 5) и соотношении катализатора и реагента 1 (0,05 - 0,2) : 1, температуре (-10) (+100)°С, лучше (-5) - (20)°С. Катализатор используют предпочтительно в виде раствора в хлористом метилене или хлороформе. Реагенты 1 и 2 растворяют в одном из растворителей: хлористом метилене, хлорбензоле, 1, 2-дихлорэтане, бензоле, сероуглероде. 6 з.п. ф-лы, 11 табл.

ОБЪЕДИНЕННАЯ ТЕХНОЛОГИЧЕСКАЯ УСТАНОВКА ИЗОМЕРИЗАЦИИ И ТРАНСАЛКИЛИРОВАНИЯ КСИЛОЛА

Изобретение относится к двум вариантам объединенного способа изомеризации и трансалкилирования ксилола. Один из вариантов включает следующие стадии: осуществляют изомеризацию потока сырья в реакторе изомеризации при условиях изомеризации, чтобы получить продукт изомеризации; осуществляют трансалкилирование потока сырья в реакторе трансалкилирования при условиях трансалкилирования, чтобы получить продукт трансалкилирования; объединяют продукт изомеризации и продукт трансалкилирования; вводят объединенный продукт в единственный сепаратор; разделяют объединенный продукт в сепараторе, чтобы получить нижний поток сепарации; и осуществляют ректификацию нижнего потока сепарации в ректификационной колонне, чтобы получить нижний поток из ректификационной колонны. Также изобретение относится к установке для осуществления способа. Использование настоящего изобретения позволяет снизить капитальные затраты на оборудование. 3 н. и 7 з.п. ф-лы, 4 ил.

ЭНЕРГОСБЕРЕГАЮЩИЙ СПОСОБ ФРАКЦИОНИРОВАНИЯ ДЛЯ РАЗДЕЛЕНИЯ ВЫХОДЯЩЕГО ПОТОКА РЕАКТОРА ПРОЦЕССОВ ПЕРЕАЛКИЛИРОВАНИЯ TOL/A9+

TRANSALKYLIERUNG IN GEGENWART VON EINEM KATALYSATORSCHLAMM.

Verfahren zur Ausfuehrung von Intra- oder Interumlagerungen von alkylaromatischen Kohlenwasserstoffen

Catalytic hydrodisproportionation and hydrodealkylation

... 1,059,524. Hydrodisproportionation and by- -drodealkylation of alkyl aromatic hydrocarbons. - MOBIL OIL CORPORATION. Oct. 24, 1963 [Oct. 24, 1962 (2); April 22, 1963 (2)], No. 42031/63. Heading C5E. Hydrodisproportionation and/or hydrodealkylation of alkyl aromatic hydrocarbons is carried out by contacting the hydrocarbons in the presence of hydrogen under conversion conditions with a catalyst comprising a crystalline aluminosilicate containing hydrogen, ammonium or quaternary ammonium ions or ions of nitrogenous .bases, having a maximum alkali metal content of 0.25 equivalents per gram atom of aluminium and having a total cation content of at least 0À5 equivalents per gram atom of aluminium. The catalyst may also contain metal cations of Groups I B -VIII,e.g. rare earth metal cations. Hydrodispropor- - tionation conditions specified are temperatures of 100-1000‹F., L.H.S.V. of 0À05-40À0 and pressures of 1-100atmos. Hydrodealkylation conditions specified, are temperatures of 1000- 1300‹ ...

PROCEDURE FOR THE PRODUCTION OF ALKYL AROMATICS

PROCEDURE FOR THE PRODUCTION OF ALKYL AROMATICS

ZEOLITE SSZ-58

A TOLUENE SELECTIVE DISPROPORTIONATION CATALYST

The present invention discloses a catalyst for toluene shape selective disproportionation, comprising: a) 45 to 95 wt% of ZSM-5 molecular sieve having an average particle size of from 0.3 to 6 µm and a molar ratio of SiO2 to Al2O3 of from 20 to 120; b) 0.01 to 30 wt% of at least one metal selected from the group consisting of Group IIB metals, Group IIIB metals, rare earth elements and Group VIII metals other than nickel, or oxide(s) thereof; c) 0 to 20 wt% of at least one metal selected from the group consisting of Group VA metals, Group VIB metals and alkaline earth metals, or oxide(s) thereof; d) 1 to 25 wt% of a silica inert surface coating derived from an organopolysiloxane; and e) 1 to 50wt% of a binder. The present invention further discloses a process for shape selectively disproportionating toluene into p-xylene, comprising contacting a reaction stream containing toluene with the catalyst for toluene shape selective disproportionation under toluene disproportionation conditions ...

HIGH ACTIVITY SMALL CRYSTAL ZSM-12

A porous, crystalline material is described having the framework structure of ZSM-12 and a composition involving the molar relationship: X2O3 :(n)YO2 wherein X is a trivalent element, Y is a tetravalent element and n is less than about 45, e.g., less than about 40, wherein the average crystal size of the material is less than about 0.1 micron, which material is substantially free of impurities. The material is made by: (a) preparing a mixture capable of forming said material, said mixture comprising sources of alkali or alkaline earth metal (M), an oxide of trivalent element (X), an oxide of tetravalent element (Y), hydroxyl (OH") ions, water, and an organic monoquaternary ammonium cation directing agent (R) and an organic diquaternary ammonium structure blocking agent (R'); (b) maintaining the mixture under sufficient conditions until crystals of said material are formed; and (c) recovering the crystalline material from step (ii). The material can be used as a hydrocarbon conversion process ...

SENSOR, E, SISTEMA CONFIGURADO PARA DETERMINAR INFORMAÇÃO RELACIONADA A UM OU MAIS ANALITOS GASOSOS EM UM CORPO DE GÁS

transalquilacao de materias-primas de hidrocarboneto aromatico pesado

MONOALKYLATED AROMATIC COMPOUND PRODUCTION

... 33 MONOALICYLATED AROMATIC COMPOUND PRODUCTION AbstractA process for producing a monoalkylated aromatic compound in an alkylation reaction zone, said process comprising the steps of: (a) providing said alkylation reaction zone with an alkylatable aromatic compound, an alkylating agent, and a catalytic particulate material; and (b) contacting said alkylatable aromatic compound and said alkylating agent with said catalytic particulate material in said alkylation reaction zone maintained under alkylation conditions, to form a product comprised of said monoallcylated aromatic compound and polyalkylated aromatic compound(s), wherein majority of said catalytic particulate material has a surface area over volume ratio of greater than about 79 cm-I.

METHOD FOR PRODUCING XYLENE

This method for producing xylene involves producing xylene from an oil feedstock, which has a 10% distillation temperature of at least 135°C and a 90% distillation temperature of not more than 380°C, and comprises: a decomposition reforming reaction step in which a monocylic aromatic hydrocarbon is produced by bringing the oil feedstock into contact with a catalyst; a separation and recovery step in which a fraction A, which contains a monocyclic aromatic hydrocarbon with a 10% distillation temperature of at least 75°C and a 90% distillation temperature of not more than 140°C, a xylene fraction containing xylene, and a fraction B, which contains a monocyclic aromatic hydrocarbon with a 10% distillation temperature of at least 145°C and a 90% distillation temperature of not more than 215°C, are separated and recovered from the product produced in the decomposition reforming reaction step; and a xylene conversion step in which a mixed fraction that is obtained by mixing the fraction A and ...

Method of conversion of heavy aromatics

A method is provided for conversion of heavy alkylaromatic compounds, particularly those in the C8-C12range, into more valuable aromatics of benzene, toluene and xylene utilizing a toluene disproportionation unit containing a nickel, palladium or platinum-modified mordenite catalyst. The method allows large amounts of these heavy alkylaromatic compounds to be processed without adversely affecting catalyst activity or catalyst life. This is accomplished by introducing the heavy alkylaromatic compounds into the reactor at constant reaction severity conditions and maintaining those conditions during conversion.

Synthesis of MCM-58

This invention provides a process for the synthesis of MCM-58 using 1-(1-adamantyl) pyridinium cations as a directing agent. The resultant MCM-58 is useful in a variety of hydrocarbon conversion reactions including toluene disproportionation, transalkylation of aromatics, reaction of paraffins with aromatics, paraffin isomerization and alkylation of aromatics with olefins.

КОМПОЗИЦИЯ КАТАЛИЗАТОРА

Изобретение относится к каталитической композиции для конверсии сырья, содержащего алкилароматические углеводороды, включающей (a) носитель, содержащий (i) цеолит типа морденита, имеющий среднюю длину кристаллитов в направлении, параллельном 12-кольцевым каналам, измеренную посредством применения уравнения Шеррера к данным дифракции рентгеновских лучей, 60 нм или менее, и объем мезопор по меньшей мере 0,10 см3/г в количестве в диапазоне от 30 до 70% масс. в пересчете на общую массу носителя, (ii) цеолит типа ZSM-5 в количестве от 15 до 60% масс. в пересчете на общую массу носителя; и (iii) неорганическое связующее в количестве в диапазоне от 10 до 40% мас. в пересчете на общую массу носителя; где цеолит типа ZSM-5 имеет среднечисловой размер кристаллов в диапазоне от 25 до 100 нм, как определено дифракцией рентгеновских лучей, и (b) от 0,1 до 10% мас. платины, причем неорганическое связующее содержит диоксид титана. Изобретение также относится к способу приготовления композиции катализатора ...

СПОСОБ ТРАНСАЛКИЛИРОВАНИЯ И ПРИМЕНЯЮЩАЯСЯ В НЕМ КАТАЛИТИЧЕСКАЯ КОМПОЗИЦИЯ

Изобретение касается способа получения моноалкилированного ароматического соединения, такого как, например, этилбензол или кумол, в котором поток алкилирующегося ароматического соединения, такого как, например, бензол, и поток алкилирующего реагента, такого как, например, полиэтилбензол или полиизопропилбензол, вводят во взаимодействие в присутствии катализатора трансалкилирования и при условиях проведения трансалкилирования по меньшей мере в частично жидкой фазе. Катализатор трансалкилирования содержит цеолит, обладающий типом каркасной структуры, выбранным из группы, включающей FAU, BEA*, MOR, MWW и их смеси. Цеолит обладает молярным отношением диоксид кремния/оксид алюминия, находящимся в диапазоне от 10 до 15. Каталитическая композиция для трансалкилирования обладает отношением площадь наружной поверхности/объем, находящимся в диапазоне от 30 до 85 см-1. Технический результат - более высокая степень превращения полиалкилированных ароматических соединений с образованием необходимого ...

СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА НА ОСНОВЕ МОЛИБДЕНА И ПЛАТИНЫ ДЛЯ СИНТЕЗА БЕНЗОЛА ПУТЕМ ТРАНСАЛКИЛИРОВАНИЯ

Изобретение относится к способу получения композиции катализатора и способу превращения алкилароматических углеводородов, включающий изготовление композиции катализатора указанным способом и приведение упомянутого исходного сырья в контакт с указанной композицией катализатора Способ получения композиции катализатора включает: (a) получение носителя, содержащего (i) морденит в количестве в диапазоне от 30 до 70% мас. в пересчете на общую массу носителя, (ii) цеолит типа ZSM-5 в количестве в диапазоне от 15 до 60% мас. в пересчете на общую массу носителя; и (iii) неорганическое связующее в количестве в диапазоне от 10 до 40% мас. в пересчете на общую массу носителя; (b) введение в носитель молибдена в количестве в диапазоне от 2 до 9% мас. в виде металла в пересчете на общую массу композиции катализатора и воздействие на обработанный таким образом носитель температуры от 100 до максимум 300 °С ; и (c) введение в молибденсодержащий носитель, полученный на стадии (b), платины в количестве от ...

СПОСОБ ПОЛУЧЕНИЯ МОЛЕКУЛЯРНОГО СИТА

Изобретение относится к синтезу цеолитов. Предложен цеолит морденит, содержащий внутри пор направляющий реагент для формирования структуры, выбранный из группы, включающей тетраэтиламмоний (ТЭА), метилтриэтиламмоний (МТЭА) и их смеси, обладающий площадью поверхности мезопор, равной более 30 м/г и до 62 м/г, и отношением площади поверхности мезопор к полной площади поверхности цеолита, равным более 0,05 и до 0,11. Цеолит содержит агломераты, состоящие из первичных кристаллитов. Кристаллиты обладают средним размером первичных кристаллов, определенным с помощью трансмиссионной электронной микроскопии, равным менее 80 нм. Предложен также способ получения цеолита. Изобретение обеспечивает получение морденита, обладающего мелкими кристаллами и большой поверхностью мезопор. 4 н. и 6 з.п. ф-лы, 12 ил., 1 табл.

СПОСОБ ПРЕВРАЩЕНИЯ СМЕСЕЙ, СОДЕРЖАЩИХ АРОМАТИЧЕСКИЕ УГЛЕВОДОРОДЫ C9 В ИЗОМЕРЫ КСИЛОЛА

Изобретение относится к способу получения изомеров ксилола (вариантам), характеризующемуся тем, что включает: (a) контактирование сырья, содержащего ароматические соединения С9, с катализатором, содержащим несульфидированный морденит, пропитанный оксидом металла VIB группы с получением потока промежуточных продуктов, содержащих изомеры ксилола; (b) выделение, по меньшей мере, части изомеров ксилола из потока промежуточных продуктов и (c) возвращение в сырье на стадию (а) потока промежуточных продуктов, обедненных изомерами ксилола, полученного на стадии (b). Также предложенное изобретение относится к вариантам способа превращения сырья, содержащего ароматические соединения C9, в ксилолы, в поток продуктов, содержащих изомеры ксилолов. Применение указанных способов приводит к высокой конверсии ароматических соединений С9 и метилэтилбензола, а также к высоким соотношениям изомеров ксилола к этилбензолу, изомеров ксилола к ароматическим соединениям С9, изомеров ксилола к ароматическим соединениям ...

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

СПОСОБ ПОЛУЧЕНИЯ ИЗОМЕРОВ КСИЛОЛА (ВАРИАНТЫ)

... 1. Способ получения изомеров ксилола, включающий контактирование сырья, содержащего ароматические углеводороды С9, на несульфидированном катализаторе в условиях, пригодных для конверсии сырья в продукт, содержащий изомеры ксилола, при этом катализатор включает носитель, импрегнированный компонентом гидрирования, носитель включает макропористое связующее и крупнопористое сито. ! 2. Способ по п.1, отличающийся тем, что сито выбрано из группы, состоящей из крупнопористых цеолитов, крупнопористых алюмофосфатов, крупнопористых кремнийалюмофосфатов и их смесей. ! 3. Способ по п.2, отличающийся тем, что крупнопористый цеолит выбран из группы, состоящей из морденита, бета-цеолита, Y-цеолита и их смесей. ! 4. Способ получения изомеров ксилола, включающий контактирование сырья, содержащего ароматические углеводороды С6-С8 и по существу свободного от С9+ ароматических углеводородов, на несульфидированном катализаторе в условиях, пригодных для конверсии сырья в продукт, содержащий изомеры ксилола, ...

СПОСОБ ПОЛУЧЕНИЯ АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ

... 1. Способ получения ароматических углеводородов с применением оксигената (кислородсодержащего соединения) в качестве исходного, включающий:i) реакцию с участием оксигената по меньшей мере в одном реакторе ароматизации и получение продукта реакции ароматизации;ii) разделение (сепарацию) продукта реакции ароматизации на сепарационной установке А, на которой, предпочтительно, осуществляются такие операции, как охлаждение, промывка щелочью и/или промывка водой и т.п., и получение потока газообразных углеводородов X и потока жидких углеводородов Y;iii) получение потока углеводородов X1, содержащего неароматические углеводороды, после удаления газа и/или части оксигената из потока газообразных углеводородов X на сепарационной установке В, на которой, предпочтительно, осуществляется короткоцикловая безнагревная адсорбция, ректификация (разгонка) и/или адсорбция; или получение потока Х2, содержащего неароматические углеводороды, и потока Х3, содержащего ароматические углеводороды, после удаления ...

Multiple zeolite catalyst

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

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

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

Process For Producing Cyclohexylbenzene

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

Processes for Transalkylating Aromatic Hydrocarbons

A process for transalkylating aromatic hydrocarbon compounds, the process comprising introducing an aromatic hydrocarbon feed stream and a sulfur source to a transalkylation zone. The feed stream contacts a catalyst in the transalkylation zone in the presence of sulfur, and produces a reaction product stream comprising benzene and xylene. The invention includes methods to control the transalkylation process.

Heavy alkylbenzene transalkylation operating cost reduction

A process for increasing the production of monoalkylbenzenes is presented. The process includes utilizing a transalkylation process to convert dialkylbenzenes to monoalkylbenzenes. The transalkylation process recycles a portion of the effluent stream from the transalkylation reactor back to the feed of the transalkylation reactor. The recycled dialkylbenzenes and a portion of the recycled benzene are converted to monoalkylbenzenes.

Production of renewable aromatic compounds

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

"process for producing cycloalkylaromatic compounds"

In a process for producing a cycloalkylaromatic compound, an aromatic compound, hydrogen and at least one diluent are supplied to a hydroalkylation reaction zone, such that the weight ratio of the diluent to the aromatic compound supplied to the hydroalkylation reaction zone is at least 1:100. The aromatic compound, hydrogen and the at least one diluent are then contacted under hydroalkylation conditions with a hydroalkylation catalyst in the hydroalkylation reaction zone to produce an effluent comprising a cycloalkylaromatic compound.

Catalysts Useful for the Alkylation of Aromatic Hydrocarbons

A catalyst useful for the alkylation or transalkylation of aromatic compounds is disclosed. The catalyst is an acid-treated zeolitic catalyst produced by a process including contacting an acidic zeolitic catalyst comprising surface non-framework aluminum and framework aluminum with an organic dibasic acid at a catalyst to acid weight ratio in the range from about 2:1 to about 20:1 and at a temperature in the range from about 50° C. to about 100° C. to selectively remove at least a portion of the surface non-framework aluminum. The resulting catalyst may have a measured first-order rate constant, k cum , for the alkylation of benzene with propylene to form cumene, of at least 2.0 cm 3 /s g.

Process for producing cumene

A process of producing isopropyl benzene which solves the problem of high amount of n-propyl benzene according to the prior art. The process separates the polyisopropyl benzene through a suitable rectification into two streams of relatively lighter and heavier components, wherein the content of diisopropylbenzene in the stream of relatively lighter components is controlled to be at least greater than 95 wt %, and the content of tri-isopropyl benzene in the stream of relatively heavier components is controlled to be at least greater than 0.5 wt %. Such a technical solution subjecting the two streams respectively to the transalkylation solves the problem raised from the prior art, and is useful for the industrial production of isopropyl benzene.

Multimetal Zeolites Based Catalyst for Transalkylation of Heavy Reformate to Produce Xylenes and Petrochemical Feedstocks

A transalkylation catalyst for the transalkylation of a heavy reformate is provided. The catalyst includes two solid acid zeolites having different physical and chemical properties, and at least three metals selected from the group 4 Lanthanoids, and the elements found in groups 6 and 10 of the periodic table. 1. A transalkylation catalyst for the conversion of a heavy reformate feedstock into a xylenes-rich product stream , the transalkylation catalyst comprising:at least two solid acid zeolites, wherein the first solid acid zeolite and the second solid acid zeolite are selected from the group consisting of mordenite, beta zeolite, ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, MFI topology zeolite, NES topology zeolite, EU-1, MAPO-36, SAPO-5, SAPO-11, SAPO-34, and SAPO-41, and wherein the first and second solid acid zeolite are not identical; andat least three metal selected from the Group 4 Lanthanoids, Group 6, and Group 10 of the Periodic Table of the Elements.2. The method of wherein the first and second solid acid zeolites are physically and chemically different.3. The method of wherein the acidity of the first or second solid acid zeolite is greater than the other.4. The method of wherein the first solid acid zeolite is Beta zeolite and the second solid acid zeolite is ZSM-5.5. The method of wherein the metals are nickel claim 1 , cerium and platinum.6. The method of wherein the pore size of the first and second solid acid zeolites are different.7. The method of wherein the first solid acid zeolite that is present in an amount of between about 10 and 90% by weight of the total catalyst weight.8. The method of claim 1 , wherein second solid acid zeolite that is present in an amount of between about 10 and 90% by weight of the total catalyst weight.9. The method of claim 1 , wherein the transalkylation catalyst further includes a binder selected from inorganic oxides.10. The method of claim 1 , wherein the metal components are present in an amount of between about 0. ...

Hydrocarbon Conversion Process Using a High Throughpout Process for Manufacturing Molecular Sieves

A method of crystallizing a crystalline molecular sieve having a pore size in the range of from about 2 to about 19 Å, said method comprising the steps of (a) providing a mixture comprising at least one source of ions of tetravalent element (Y), at least one hydroxide source (OH − ), and water, said mixture having a solid-content in the range of from about 15 wt. % to about 50 wt. %; and (b) treating said mixture to form the desired crystalline molecular sieve with stirring at crystallization conditions sufficient to obtain a weight hourly throughput from about 0.005 to about 1 hr −1 , wherein said crystallization conditions comprise a temperature in the range of from about 200° C. to about 500° C. and a crystallization time less than 100 hr.

Low pressure transalkylation process

A process for transalkylation is described. The process operates at a lower pressure than a typical transalkylation processes, and provides higher benzene purity with comparable or lower ring loss compared to the typical transalkylation process. The xylene selectivity is comparable to or higher than the standard process, and the ethyl benzene selectivity is comparable to or lower than the standard process.

PROCESS FOR PREPARING LINEAR ALKYL BENZENE

The present disclosure relates to a process for preparing linear alkyl benzne (LAB). The process comprises alkylation of benzene with an alkylating agent in the presence of an ionic liquid to obtain a first product mixture comprising a first organic phase and a first aqueous phase comprising first partially spent ionic liquid. The first organic phase is deacidified and fractionally distilled to obtain a fraction comprising LAB and a fraction comprising HAB. The fraction comprising HAB is transalkylated with benzene in the presence of the ionic liquid to obtain a second product mixture comprising a second organic phase comprising LAB and a second aqueous phase comprising second partially spent ionic liquid. The partially spent ionic liquids are regenerated, and reused in the steps of alkylation or transalkylation for at least 6 cycles. 1. A process for preparing linear alkyl benzene by alkylation of benzene , said process comprising the following steps:a) alkylating benzene with an alkylating agent in the presence of an ionic liquid to obtain a first product mixture;b) allowing the first product mixture to settle to obtain a first biphasic mixture comprising a first organic phase and a first aqueous phase, wherein the first organic phase comprises linear alkyl benzene (LAB), heavier alkyl benzene (HAB) and unreacted benzene, and the first aqueous phase comprises first partially spent ionic liquid;c) deacidifying the first organic phase to obtain a deacidified first organic phase;d) fractionally distlling the deacidified first organic phase to obtain a fraction comprising unreacted benzene, a fraction comprising LAB and a fraction comprising HAB;e) transalkylating the fraction comprising HAB with benzene in the presence of the ionic liquid at a temperature in the range of 70° C. to 120° C. to obtain a second product mixture;f) allowing the second product mixture to settle to obtain a second biphasic mixture comprising a second organic phase and a second aqueous phase; ...

Process for producing ethylbenzene

A process for producing ethylbenzene is described in which benzene and ethylene are supplied to an alkylation reaction zone. Also added to the alkylation reaction zone is a C 3+ olefin in an amount of at least 200 ppm by weight of the ethylene supplied to the alkylation reaction zone. The benzene, ethylene and C 3+ olefin are contacted with an alkylation catalyst in the alkylation reaction zone to alkylate at least part of the benzene and produce an alkylation effluent comprising ethylbenzene, polyethylated benzene and at least one mono-C 3+ alkyl benzene. The alkylation effluent is separated into a first product fraction comprising ethylbenzene and a second fraction comprising polyethylated benzene and the at least one mono-C 3+ alkyl benzene. The second fraction is then contacted with benzene in the presence of a transalkylation catalyst to convert at least part of the polyethylated benzene to ethylbenzene and produce a transalkylation effluent.

Processes for Converting Aromatic Hydrocarbons via Alkyl-Demethylation

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

CONVERSION OF WASTE PLASTIC THROUGH PYROLYSIS TO HIGH VALUE PRODUCTS LIKE BENZENE AND XYLENES

A process for producing benzene and xylenes comprising introducing hydrocarbon liquid stream to hydroprocessor to yield first gas stream and hydrocarbon product (C+); optionally introducing hydrocarbon product to first aromatics separating unit to produce saturated hydrocarbons (C+) and first aromatics stream (C+); feeding hydrocarbon product and/or saturated hydrocarbons to reformer to produce reformer product, second gas stream, and hydrogen stream; introducing reformer product to second aromatics separating unit to produce a non-aromatics recycle stream and second aromatics stream comprising C+ aromatics; recycling non-aromatics recycle stream to reformer; introducing first aromatics stream and/or second aromatics stream to third aromatics separating unit to produce first Caromatics (benzene), Caromatics (toluene), Caromatics (xylenesðylbenzene), C 1. A process for producing benzene and xylenes comprising:{'sub': '5', '(a) contacting a hydrocarbon liquid stream with a hydroprocessing catalyst in the presence of hydrogen in a hydroprocessing unit to yield a hydrocarbon product and a first gas stream, wherein the hydrocarbon product comprises C+ hydrocarbons;'}{'sub': 5', '6, '(b) optionally introducing at least a portion of the hydrocarbon product to a first aromatics separating unit to produce a saturated hydrocarbons stream and a first aromatics stream, wherein the saturated hydrocarbons stream comprises C+ saturated hydrocarbons, and wherein the first aromatics stream comprises C+ aromatic hydrocarbons;'}{'sub': 6', '8', '6', '8, '(c) feeding at least a portion of the hydrocarbon product and/or at least a portion of the saturated hydrocarbons stream to a reforming unit to produce a reforming unit product, a second gas stream, and a hydrogen stream, wherein the reforming unit comprises a reforming catalyst, and wherein an amount of Cto Caromatic hydrocarbons in the reforming unit product is greater than an amount of Cto Caromatic hydrocarbons in the saturated ...

Catalyst System and Use in Heavy Aromatics Conversion Processes

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

PROCESSES AND APPARATUSES FOR PREPARING AROMATIC COMPOUNDS

Processes and apparatuses for preparing aromatic compounds are provided herein. In an embodiment, a process for preparing aromatic compounds includes providing a first stream that includes an aromatic component, a non-aromatic component, and a sulfur-containing component. The aromatic component and the sulfur-containing component are separated from the non-aromatic component of the first stream to form a separated aromatic stream and a raffinate stream. The separated aromatic stream includes the aromatic component and the sulfur-containing component. The raffinate stream includes the non-aromatic component. The separated aromatic stream is concurrently transalkylated and desulfurized in the presence of a catalyst that includes acid function and metal function to produce a transalkylated aromatic stream and a sulfur-containing gas stream that is separate from the transalkylated aromatic stream. 1. A process for preparing aromatic compounds , the process comprising the steps of:providing a first stream comprising an aromatic component, a non-aromatic component, and a sulfur-containing component;separating the aromatic component and the sulfur-containing component from the non-aromatic component of the first stream to form a separated aromatic stream comprising the aromatic component and the sulfur-containing component and a raffinate stream comprising the non-aromatic component;concurrently transalkylating and desulfurizing the separated aromatic stream in the presence of a catalyst that includes acid function and metal function to produce a transalkylated aromatic stream and a sulfur-containing gas stream separate from the transalkylated aromatic stream.2. The process of claim 1 , wherein providing the first stream comprises fractionating a full boiling range naphtha stream comprising the sulfur-containing component into a fractionation overhead stream comprising compounds having 5 or less carbon atoms claim 1 , a fractionation bottoms stream comprising compounds ...

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

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

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

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

PROCESS FOR MAKING XYLENES AND PHENOL FROM COAL DERIVED LIQUIDS

Processes and apparatus for making xylenes and phenol are described. Phenol and alkyl phenols are separated from coal derived liquid. The phenol is separated from the alkyl phenols. The alkyl phenols can be reacted with aromatics such as benzene and toluene to make xylenes. The xylenes and other aromatics are then separated from the phenol and alkyl phenols. Para-xylene is separated and recovered using a xylene separation process, and meta-xylene and ortho-xylene are optionally converted to para-xylene through an isomerization reaction. 1. A process for making xylenes and phenol comprising:providing a first phenols stream comprising phenol and alkyl phenols from a coal derived liquid;separating the first phenols stream into at least a phenol product stream comprising phenol, and a cresols stream comprising cresols in a phenols separation zone;transalkylating the cresols stream with a first aromatics stream comprising toluene, benzene, or both in a cresols transalkylation reaction zone in the presence of a cresols transalkylating catalyst to form a first effluent stream comprising aromatics, phenol, and alkyl phenols;separating the first effluent stream into at least a second aromatics stream comprising aromatics and a second phenols stream comprising phenol and alkyl phenols in a phenols and aromatics separation zone;separating the second aromatics stream into at least the first aromatics stream and a first xylenes stream comprising para-xylene, ortho-xylene, and meta-xylene in an aromatics separation zone; andintroducing the second phenols stream into the phenols separation zone.2. The process of wherein separating the first phenols stream into at least the phenol product stream claim 1 , and the cresols stream comprises separating the first phenols stream into at least the phenol product stream claim 1 , the cresols stream claim 1 , and a xylenols stream comprising xylenols; wherein the first aromatics stream comprises toluene; and wherein separating the second ...

Xylene Production Processes and Systems

A process and related system for producing para-xylene (PX). In an embodiment, the process includes (a) separating a feed stream comprising C aromatic hydrocarbons into a toluene containing stream and a C hydrocarbon containing stream and (b) contacting at least part of the toluene containing stream with a methylating agent in a methylation unit to convert toluene to xylenes and produce a methylated effluent stream. In addition, the process includes (c) recovering PX from the methylated effluent stream in (b) to produce a PX depleted stream and (d) transalkylating the PX depleted stream to produce a transalkylation effluent stream. The transalkylation effluent stream includes a higher concentration of toluene than the PX depleted stream. Further, the process includes (e) converting at least some ethylbenzene (EB) within the C hydrocarbon containing stream into toluene and (f) flowing the toluene converted in (e) to the contacting in (b). 1. A process for producing para-xylene (PX) , the process comprising:{'sub': 6+', '8+, '(a) separating a feed stream comprising C aromatic hydrocarbons into at least a toluene containing stream and a C hydrocarbon containing stream;'}(b) contacting at least part of the toluene containing stream with a methylating agent in a methylation unit under conditions effective to convert toluene to xylenes and produce a methylated effluent stream;(c) recovering PX from the methylated effluent stream in (b) to produce a PX depleted stream;(d) transalkylating the PX depleted stream to produce a transalkylation effluent stream, wherein the transalkylation effluent stream includes a higher concentration of toluene than the PX depleted stream;{'sub': '8+', '(e) converting at least some ethylbenzene (EB) within the C hydrocarbon containing stream into toluene; and'}(f) flowing the toluene converted in (e) to the contacting in (b).2. The process of claim 1 , further comprising:{'sub': 7', '8+, '(g) separating from the transalkylation effluent stream ...

SYSTEMS AND METHODS OF PRODUCING AROMATIC PRODUCTS

Systems and methods for producing aromatic products are provided. An aromatic stream is provided with aromatic compounds and olefins. The olefins are reacted with aromatic compounds to form colored bodies, and the aromatic stream is distilled to produce an overhead stream and reboiler stream. The colored bodies are in the reboiler stream, and the reboiler stream is passed through an absorbent to remove the colored bodies. 1. A method of producing toluene , the method comprising the steps of:processing a feed naphtha stream with a naphtha processing unit to produce a processed naphtha stream;separating the processed naphtha stream into an aromatic stream and a non-aromatic stream, wherein the aromatic stream primarily comprises toluene and benzene;reacting olefins remaining in the aromatic stream to produce colored bodies;distilling the aromatic stream to produce an overhead stream and a reboiler stream, wherein the reboiler stream comprises toluene and colored bodies; andremoving the colored bodies from the reboiler stream by passing the reboiler stream through an absorbent, wherein the absorbent selectively absorbs colored bodies over toluene.2. A method of producing aromatic products , the method comprising the steps of:providing an aromatic stream, where the aromatic stream comprises aromatic compounds and olefins;reacting the olefins with the aromatic compounds in the aromatic stream to form colored bodiesdistilling the aromatic stream to produce an overhead stream and a reboiler stream, wherein the reboiler stream comprises the colored bodies; andpassing the reboiler stream through an absorbent to remove the colored bodies.3. The method of where providing the aromatic stream further comprises providing an aromatic stream primarily comprising benzene and toluene.4. The method of wherein providing the aromatic stream further comprises processing a feed naphtha stream with a reforming process claim 3 , wherein aromatic compounds are produced in the reforming ...

Selective catalyst for hydrogenolysis of ethyl-aromatics by conserving methyl-aromatics

The present invention relates to a hydrogenolysis process wherein a hydrocarbon-based feedstock comprising aromatic compounds having at least 8 carbon atoms is treated by means of a hydrogen feed and in the presence of a catalyst, in order to convert C2+ alkyl chains of said aromatic compounds into methyl groups and to produce a hydrogenolysis effluent enriched in methyl-substituted aromatic compounds, wherein the catalyst comprises a support, comprising at least one refractory oxide, and an active phase comprising nickel and molybdenum, wherein: the nickel content being between 0.1 and 25% by weight relative to the total weight of the catalyst; the molybdenum content being between 0.1 and 20% by weight relative to the total weight of the catalyst; and the catalyst comprising a molar ratio of molybdenum to nickel of between 0.2 and 0.9. The present invention also relates to said catalyst and to the process for preparing said catalyst.

Methods and Systems of Upgrading Heavy Aromatics Stream to Petrochemical Feedstock

Provided here are systems and methods that integrate a hydrodearylation process and a transalkylation process into an aromatic recovery complex. Various other embodiments may be disclosed and claimed. 1. A system for conversion of alkyl-bridged non-condensed alkyl multi-aromatic compounds to alkyl mono-aromatic compounds , the system comprising:{'sub': 9', '10, 'a first separator adapted to receive a feed stream containing one or more of heavy alkyl aromatic compounds and one or more alkyl-bridged non-condensed alkyl multi-aromatic compounds having at least two benzene rings connected by an alkyl bridge group with at least two carbons and the benzene rings being connected to different carbons of the alkyl bridge group, and produces a first product stream containing Cand Ccompounds and a second product stream containing one or more of heavy alkyl aromatic compounds and alkyl-bridged non-condensed alkyl multi-aromatic compounds;'}a hydrodearylation reactor fluidly coupled to the first separator and adapted to receive a hydrogen stream and the second product stream and to produce a third product stream in presence of a catalyst, the third product stream containing one or more alkyl mono-aromatic compounds; and{'sub': 8', '9+, 'a second separator fluidly coupled to the hydrodearylation reactor and adapted to receive the third product stream and to produce a benzene-containing stream, a toluene-containing stream, a C-rich stream, and a bottoms C stream.'}2. The system of claim 1 , further comprising:{'sub': '9+', 'a transalkylation unit fluidly coupled to the second separator and adapted to receive the first product stream and one or more of the benzene-containing stream, the toluene-containing stream, and the bottoms C stream, and to produce alkyl mono-aromatic compounds.'}3. The system of claim 1 , further comprising:{'sub': '8', 'a para-xylene unit fluidly coupled to the second separator and adapted to receive the C-rich stream and to produce a para-xylene-rich stream ...

Process for Transalkylation of Aromatic Fluids

Systems and methods are provided for an improved transalkylation process that better tolerates the presence of Caromatics and may be conducted substantially in the liquid phase. The transalkylation feedstock may comprise alkyl-substituted benzenes and naphthalene and the transalkylation effluent comprises alkyl-substituted naphthalene and benzene, toluene, and/or xylenes. 1. A method for liquid phase transalkylation of aromatic compounds , comprising:exposing an aromatic feedstock comprising at least about 1.0 wt % naphthalene and alkyl-substituted benzene to a transalkylation catalyst under effective transalkylation conditions to form a transalkylation effluent comprising an alkyl-substituted naphthalene and benzene;wherein a mole fraction of aromatic compounds in the liquid phase, relative to the total amount of aromatic compounds in the feedstock, is at least about 0.01 under the effective transalkylation conditions; and a first molecular sieve having an MWW framework with an n value of about 2 to about 50;', 'a second molecular sieve corresponding to a Beta polymorph with an n value of about 10 to about 60; and', 'a third molecular sieve having a FAU framework with an n value of about 2 to about 400;', {'sub': 2', '2', '3, 'where n is a molar ratio YOover XOin the framework of the first, second, and third molecular sieves, X is a trivalent element, and Y is a tetravalent element.'}], 'wherein the transalkylation catalyst comprises at least one of the following2. The method of claim 1 , wherein the transalkylation catalyst further comprises 0.01 wt % to 5 wt % of a metal from Groups 5-11 and 14 supported on the transalkylation catalyst.3. The method of claim 2 , wherein the metal from Groups 5-11 and 14 is selected from the group consisting of Pd claim 2 , Pt claim 2 , Ni claim 2 , Rh claim 2 , Sn claim 2 , or a combination thereof.4. The method of claim 1 , wherein the MWW framework of the first molecular sieve is selected from the group consisting of MCM-22 ...

COUPLING OF UNIT FOR EXTRACTING METHYL-SUBSTITUTED AROMATICS WITH UNIT FOR HYDROGENOLYSING ALKYL-AROMATICS

The present invention relates to a device and a process for converting aromatic compounds, wherein: methyl-substituted aromatic compounds are extracted from a hydrocarbon feedstock () comprising aromatic compounds having at least 8 carbon atoms in an extraction unit (), to produce at least one effluent enriched in methyl-substituted aromatic compounds (A, B) and an effluent depleted in methyl-substituted aromatic compounds (); and C2+ alkyl chains of the aromatic compounds of the depleted effluent () are converted into methyl groups in a hydrogenolysis unit () placed downstream of the extraction unit (), to produce a hydrogenolysis effluent enriched in methyl-substituted aromatic compounds ().

PROCESS FOR THE PRODUCTION OF HIGH PURITY PARA-XYLENE AND HIGH PURITY TOLUENE

A process for the production of high purity toluene and para-xylene is described. More specifically, the process involves the production of high purity toluene produced via a light-desorbent selective adsorption process for para-xylene production, such as light desorbent para-xylene extraction, without the need for dedicated solvent extraction or olefin removal from the toluene stream. 1. A process for producing high purity toluene and para-xylene in a para-xylene complex comprising:separating an extract stream comprising para-xylene and toluene from an adsorbent chamber into an overhead stream comprising C6− compounds and a bottoms stream comprising para-xylene and toluene in a first para-xylene fractionation column;separating the bottoms stream from the first para-xylene fractionation column in a second para-xylene fractionation column into a sidedraw stream comprising high purity para-xylene, an overhead stream comprising toluene, and a bottoms stream comprising C9+ aromatics;recovering the sidedraw stream as a high purity para-xylene stream; andrecovering at least a portion of the overhead stream from the second para-xylene fractionation column as a high purity toluene product stream.2. The process of wherein the overhead stream from the second para-xylene fractionation column comprises high purity toluene.3. The process of further comprising;separating the overhead stream from the second para-xylene fractionation column in a toluene fractionation column into an overhead stream comprising high purity toluene and a bottom stream comprising xylenes, and wherein the high purity toluene product stream comprises the overhead stream from the toluene fractionation column.4. The process of further comprising:introducing a mixed xylenes stream and a toluene stream into the adsorption chamber comprising a para-xylene selective adsorbent; andseparating the mixed xylenes stream and the toluene stream into the extract stream and a stream comprising ortho-xylene, meta-xylene, ...

Energy Efficient Fractionation Process for Separating the Reactor Effluent from TOL/A9+ Transalkylation Processes

Processes and apparatus are disclosed for the energy efficient separation of the effluent from a TOL/A9+ transalkylation reactor. The apparatus includes a reboiled prefractionation column and a sidedraw tower that produces: 1) an overhead stream including unreacted toluene, 2) a stream including unreacted C9+ aromatics, a portion of which stream may be recycled to the reactor; and 3) a sidedraw stream including C8 aromatics that may be directed to a crystallization or selective adsorption paraxylene separation unit for recovery o a paraxylene product.

Transalkylated Cyclohexylbenzyl and Biphenyl Compounds

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

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 ...

Alkylated Aromatics Production

Disclosed is a process for the production of alkylated aromatics by contacting a feed stream comprising an alkylatable aromatic, an alkylating agent and trace amounts of water and impurities in the presence of a first catalyst and an alkylation catalyst wherein such water and impurities are removed in order to improve the cycle length of such alkylation catalysts. Water and at least a portion of impurities are removed in a dehydration zone. A reaction zone having a first catalyst which, in some embodiments is a large pore molecular sieve, acts to remove another portion of impurities, such as nitrogenous and other species. An alkylation zone having an alkylation catalyst which, in some embodiments is a medium pore molecular sieve or a MCM-22 family material, acts to remove additional impurities, and to alkylate the alkylatable aromatic compound.

PROCESS FOR XYLENE PRODUCTION WITH ENERGY OPTIMIZATION

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit. 1. A method for producing mixed xylenes from a heavy reformate feed , the method comprising the steps of:introducing the heavy reformate feed to a feed exchanger to produce a hot feed stream, wherein the feed exchanger increases the temperature of the heavy reformate feed, wherein the heavy reformate comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas;mixing the hot feed stream and a hydrogen feed to produce a mixed feed;increasing a temperature of the mixed feed in a feed-effluent exchanger to produce a hot mixed feed, wherein a temperature of the hot mixed feed is between 324 deg C. and 344 deg C.;increasing the temperature of the hot mixed feed in a feed fired heater to produce a hot reactor feed, wherein a temperature of the hot reactor feed is between 380 deg C. and 400 deg C.;introducing the hot reactor feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst;reacting the heavy reformate feed with ...

PROCESS FOR MAKING PHENOL AND XYLENES

Processes for making phenol and xylenes from a phenols-containing feed are described. The processes involve transalkylation of alkylphenols to form phenol and alkylbenzenes. The phenol is separated from the alkylbenzenes, and the alkylbenzenes may be separated into benzene, toluene, xylenes, and heavy alkylbenzene streams. The benzene stream may be recycled to the transalkylation reaction zone. The toluene may be sent to a disproportionation reaction zone, and the product is sent back to the aromatic separation zone. The toluene can also be recycled to the transalkylation zone. The xylenes are separated into a p-xylene stream and a mixed xylene stream comprising m-xylene and o-xylene. The mixed xylene stream is isomerized and the isomerized product is sent back to the aromatic separation zone. The heavy alkylbenzenes are dealkylated and separated, with the aromatic stream being recycled to the aromatic separation zone. 1. A process for producing one or more of phenol , and xylenes comprising:introducing a phenols containing feed stream into a feed separation zone;separating the phenols containing feed stream in the feed separation zone into at least a phenol stream comprising phenol, and an alkylphenol stream comprising alkylphenols;transalkylating the alkylphenol stream and a reactant stream comprising one or more of benzene or toluene in a transalkylation reaction zone under transalkylation reaction conditions to produce a transalkylation effluent stream comprising phenols, and alkylbenzenes;separating the transalkylation effluent stream in a phenol separation zone into a phenol recycle stream comprising phenols, and an aromatic stream comprising benzene, toluene, xylenes, and heavy alkylbenzenes;separating the aromatic stream in an aromatic separation zone into at least a recycle stream comprising one or more of benzene or toluene, a heavy alkylbenzene stream comprising heavy alkylbenzenes, and a mixed xylene stream comprising mixed xylenes;separating the mixed ...

PROCESSES FOR REFORMING AND TRANSALKYLATING HYDROCARBONS

Processes for reforming and transalkylating hydrocarbons are disclosed. A method for processing a hydrocarbon stream includes the steps of separating para-xylene from a first mixed-xylene and ethylbenzene-containing stream to produce a first non-equilibrium xylene and ethylbenzene stream and isomerizing the first non-equilibrium xylene and ethylbenzene stream to produce additional para-xylene. The method further includes transalkylating a toluene stream to produce a second mixed-xylene and ethylbenzene-containing stream, separating para-xylene from the second mixed-xylene and ethylbenzene-containing stream to produce a second non-equilibrium xylene and ethylbenzene stream, and isomerizing the second non-equilibrium xylene and ethylbenzene stream using a liquid phase isomerization process to produce additional para-xylene. 1. A process for processing a hydrocarbon stream comprising the steps of:separating para-xylene from the first mixed-xylene and ethylbenzene-containing stream to produce a first non-equilibrium xylene and ethylbenzene stream;isomerizing the first non-equilibrium xylene and ethylbenzene stream to produce additional para-xylene;transalkylating a toluene stream to produce a second mixed-xylene and ethylbenzene-containing stream;separating para-xylene from the second mixed-xylene and ethylbenzene-containing stream to produce a second non-equilibrium xylene and ethylbenzene stream; andisomerizing the second non-equilibrium xylene and ethylbenzene stream using a liquid phase isomerization process to produce additional para-xylene.2. The process of claim 1 , wherein the first mixed-xylene and ethylbenzene-containing stream comprises a greater proportion of ethylbenzene than does the second mixed-xylene and ethylbenzene-containing stream.3. The process of claim 1 , further comprising reforming a naphtha-containing hydrocarbon stream to produce the first mixed-xylene and ethylbenzene-containing stream and the toluene stream.4. The process of claim 3 , ...

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.

PROCESS FOR INCREASING XYLENE ISOMER TO BENZENE RATIO

Apparatuses and processes are provided for regulating C7 and C8 feed to an aromatics complex to increase the ratio of a selected xylene isomer to benzene ratio. Reformate may be split into three cuts in a splitter column. A side cut stream comprises predominantly C7 hydrocarbons and a bottoms steam from the splitter column comprises predominantly C8+ hydrocarbons. The relative proportion of the C7 and C8+ hydrocarbon streams sent to the aromatics complex are metered to determine the resulting ratio of a selected xylene isomer to benzene produced by the aromatics complex. 1. A process for preparing a feed for an aromatics complex comprising:fractionating a naphtha stream to provide a C7 stream and a C8+ aromatics stream;feeding a first C7 stream taken from the C7 stream to the aromatics complex;feeding a first C8+ aromatics stream taken from the C8+ aromatics stream to the aromatics complex; andfeeding a second C7 stream taken from the C7 stream away from the aromatics complex; orfeeding a second C8+ aromatics stream taken from the C8+ aromatics stream away from the aromatics complex.2. The process of comprising feeding the first C7 stream taken from the C7 stream to an aromatics extraction unit in the aromatics complex to extract a C7 raffinate stream from a toluene stream.3. The process of comprising feeding the C7 raffinate stream to a gasoline pool.4. The process of comprising calculating a selected xylene isomer to benzene ratio and changing a flow rate of the second C7 stream and/or the second C8+ aromatics stream in response to the calculated selected xylene isomer to benzene ratio.5. The process of comprising fractionating said C8+ aromatics stream to provide said first stream of the C8+ aromatics stream comprising C8 aromatics and said second stream of the C8+ aromatics stream comprising C9 aromatics.6. The process of comprising fractionating the toluene stream to separate a benzene stream from a concentrated toluene stream.7. The process of comprising ...

CATALYST COMPOSITION

A catalyst composition comprising (a) carrier comprising (i) 5 to 95 wt % mordenite type zeolite having a mean crystallite length parallel to the direction of the 12-ring channels of 60 nm or less and a mesopore volume of at least 0.10 cc/gram, (ii) 5 to 95 wt % ZSM-5 type zeolite; and (iii) 10 to 60 wt % inorganic binder; and (b) 0.001 to 10 wt % of one or more catalytically active metals, wherein the inorganic binder comprises titania, its preparation and its use in alkylaromatic conversion. 1. A catalyst composition comprising(a) a carrier comprising (i) mordenite type zeolite having a mean crystallite length parallel to the direction of the 12-ring channels of 60 nm or less and a mesopore volume of at least 0.10 cc/gram in an amount in the range of from 5 to 95 wt %, based on total weight of carrier, (ii) ZSM-5 type zeolite in an amount of from 5 to 95 wt %, based on total weight of carrier; and (iii) an inorganic binder in an amount in the range of from 10 to 60 wt %, based on total weight of carrier; and(b) of from 0.001 to 10 wt % of one or more catalytically active metals, wherein the inorganic binder comprises titania.2. The catalyst composition according to claim 1 , in which the carrier comprises mordenite type zeolite in an amount in the range of from 20 to 90 wt % claim 1 , based on total weight of carrier.3. The catalyst composition according to claim 1 , in which the carrier comprises ZSM-5 type zeolite in an amount of from 10 to 70 wt % claim 1 , based on total weight of carrier.4. The catalyst composition according to claim 1 , wherein the ZSM-5 type zeolite has a silica to alumina molar ratio in the range of from 15 to 40.5. The catalyst composition according to claim 1 , wherein the ZSM-5 type zeolite has a number average crystal size in the range of from 25 to 200 nm claim 1 , as determined by X-ray diffraction.6. The catalyst composition according to claim 1 , wherein the ZSM-5 type zeolite has a number average.7. A crystal size in the range of ...

Production of aromatics by reverse water gas shift, fermentation and recycling to pyrolysis.

Device and process for the conversion of a feedstock of aromatic compounds, in which the feedstock is treated notably by means of a fractionation train (4-7), a xylene separation unit (10) and an isomerization unit (11), and in which a pyrolysis unit (13) treats a second hydrocarbon feedstock, produces a pyrolysis effluent feeding the feedstock, and produces a pyrolysis gas comprising CO, CO2 and H2; a reverse water gas shift RWGS reaction section (50) treats the pyrolysis gas and produces an RWGS gas enriched in CO and in water; a fermentation reaction section (52) treats the RWGS gas enriched in CO and in water, to produce ethanol and recycle the ethanol to the inlet of the pyrolysis unit.

Crystalline Germanosilicate Materials Of New CIT-13 Topology And Methods Of Preparing The Same

The present disclosure is directed to the use of novel crystalline germanosilicate compositions in affecting a range of organic transformations. In particular, the crystalline germanosilicate compositions are extra-large-pore compositions, designated CIT-13 possessing 10- and 14-membered rings. 2. The process of comprising:(c) cracking, hydrocracking, or dehydrogenating a hydrocarbon;(d) dewaxing a hydrocarbon feedstock;(d) converting paraffins to aromatics:(e) isomerizing or disproportionating an aromatic feedstock;(f) alkylating an aromatic hydrocarbon;(g) oligomerizing an alkene;(i) separating and sorbing a lower alkane from a hydrocarbon feedstock;(j) isomerizing an olefin;(k) producing a higher molecular weight hydrocarbon from lower molecular weight hydrocarbon; or(l) reforming a hydrocarbon.3. The process of comprising converting synthesis gas containing hydrogen and carbon monoxide to a hydrocarbon stream using a catalyst comprising the crystalline microporous germanosilicate composition and a Fischer-Tropsch catalyst.4. The process of comprising reducing the concentration of an organic halide in an initial hydrocarbon product claim 1 , the initial hydrocarbon product containing an undesirable level of the organic halide claim 1 , the process comprising contacting at least a portion of the initial hydrocarbon product with a composition comprising the crystalline microporous germanosilicate composition claim 1 , under organic halide absorption conditions to reduce the halogen concentration in the hydrocarbon.6. The process of claim 1 , wherein the crystalline microporous germanosilicate composition exhibits a powder X-ray diffraction (XRD) pattern exhibiting at least seven of the characteristic peaks at 6.45±0.2 claim 1 , 7.18±0.2 claim 1 , 12.85±0.2 claim 1 , 18.26±0.2 claim 1 , 18.36±0.2 claim 1 , 18.63±0.2 claim 1 , 20.78±0.2 claim 1 , 21.55±0.2 claim 1 , 23.36±0.2 claim 1 , 24.55±0.2 claim 1 , 26.01±0.2 claim 1 , and 26.68±0.2 degrees 2-θ.7. The process ...

PROCESSES USING MOLECULAR SIEVE SSZ-96

The present disclosure is directed to processes using a new crystalline molecular sieve designated SSZ-96, which is synthesized using a 1-butyl-1-methyl-octahydroindolium cation as a structure directing agent. 2. The process of claim 1 , wherein the molecular sieve has a mole ratio of at least 10 of (1) silicon oxide to (2) and oxide selected from boron oxide claim 1 , aluminum oxide claim 1 , gallium oxide claim 1 , indium oxide claim 1 , and mixtures thereof.4. The process of claim 3 , wherein T is selected from the group consisting of Si claim 3 , Ge claim 3 , and mixtures thereof.5. The process of claim 4 , wherein T is Si.6. The process of claim 3 , wherein X is selected from the group consisting of B claim 3 , Al claim 3 , Ga claim 3 , In claim 3 , and mixtures thereof.7. The process of claim 3 , wherein T is Si and X is Al.8. The process of claim 1 , wherein the process is a process selected from the group consisting of hydrocracking claim 1 , dewaxing claim 1 , catalytic cracking claim 1 , aromatics formation claim 1 , isomerization claim 1 , alkylation and transalkylation claim 1 , conversion of paraffins to aromatics claim 1 , isomerization of olefins claim 1 , xylene isomerization claim 1 , oligomerization claim 1 , condensation of alcohols claim 1 , methane upgrading and polymerization of 1-olefins.9. The process of claim 8 , wherein the process is a dewaxing process comprising contacting the catalyst with a hydrocarbon feedstock under dewaxing conditions.10. The process of claim 1 , wherein the process is a process for producing a C lube oil from a C olefin feed comprising isomerizing the olefin feed under isomerization conditions over the catalyst. The present disclosure relates to processes using a new molecular sieve designated SSZ-96, wherein the molecular sieve is synthesized using a 1-butyl-1-methyl-octahydroindolium cation as a structure directing agent (“SDA”).Because of their unique sieving characteristics, as well as their catalytic properties ...

PROCESS FOR PRODUCING BENZENE FROM C5-C12 HYDROCARBON MIXTURE

The present invention relates to a process for producing benzene comprising the steps of: a) separating a source feedstream comprising C5-C12 hydrocarbons including benzene and alkylbenzenes into a first feedstream comprising a higher proportion of benzene than the source feedstream and a second feedstream comprising a lower proportion of benzene than the source feedstream and subsequently, b) contacting the first feedstream in the presence of hydrogen with a first hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 Å and a silica (SiO2) to alumina (Al2O3) molar ratio of 5-200 under first process conditions to produce a first product stream comprising benzene, wherein the first process conditions include a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h, and c) contacting the second feedstream with hydrogen under second process conditions to produce a second product stream comprising benzene, wherein i) the second process conditions are suitable for hydrocracking and step (c) involves contacting the second feedstream in the presence of hydrogen with a second hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 Å and a silica (SiO2) to alumina (Al2O3) molar ratio of 5-200 under the second process conditions which include a temperature of 300-600° C., a pressure of 300-5000 kPa gauge and a Weight Hourly space Velocity of 0.1-15 h, ii) the second process conditions are suitable for toluene disproportionation and involve contracting the second feedstream with a toluene disproportionation catalyst, or iii) the second process conditions are suitable for hydrodealkylation. 1. A process for producing benzene comprising the steps of:(a) separating a source feedstream comprising C5-C12 hydrocarbons including benzene and ...

Scm-11 molecular sieve, process for producing same and use thereof

The present invention relates to an SCM-11 molecular sieve, a process for producing same and use thereof. The molecular sieve has an empirical chemical composition as illustrated by the formula “the first oxide·the second oxide”, wherein the ratio by molar of the first oxide to the second oxide is more than 2, the first oxide is silica, the second oxide is at least one selected from the group consisting of germanium dioxide, alumina, boron oxide, iron oxide, gallium oxide, titanium oxide, rare earth oxides, indium oxide and vanadium oxide. The molecular sieve has specific XRD pattern, and can be used as an adsorbent or a catalyst for converting an organic compound.

Transalkylation with Reduced Ring Loss

A transalkylation process co-feeds benzene at a relatively high proportion with C9+ aromatics in a feed stream to a transalkylation reactor. At lower proportions (≤5 wt %) of benzene, ring loss is greater for benzene than toluene and ring loss is increased by increasing the proportion of benzene in the feed stream. When the benzene is co-fed in a proportion sufficiently greater than 5 weight percent of the feed stream, ring loss is unexpectedly reduced. 1. A transalkylation process comprising:(a) supplying a molecular hydrogen stream and a feed stream, the feed stream comprising C9+ heavy aromatics and optionally further comprising toluene, to a transalkylation reactor comprising therein a catalyst comprising a zeolite and at least one metal, to produce C8 aromatics; and(b) co-feeding benzene in the feed stream in a proportion of the feed stream sufficiently high to reduce ring loss relative to a reference stream at same transalkylation conditions of pressure, WHSV, inlet temperature, and molecular hydrogen to hydrocarbon molar ratio, where benzene in the feed stream is replaced with an equal weight of toluene in the reference stream.2. A transalkylation process comprising:(a) supplying a molecular hydrogen stream and a feed stream, the feed stream comprising C9+ heavy aromatics and optionally further comprising toluene, to a transalkylation reactor comprising therein a catalyst comprising a zeolite and at least one metal, to produce C8 aromatics; and(b) co-feeding benzene in the feed stream, wherein a proportion of co-fed benzene in the feed stream is not less than 10 weight percent of the total weight of aromatics in the feed stream.3. The transalkylation process of claim 1 , wherein a proportion of co-fed benzene in the feed stream is in a range from 10 to 50 weight percent of the total weight of aromatics in the feed stream.4. The transalkylation process of claim 1 , wherein the feed stream comprises a weight ratio of benzene to toluene of at least 1:1 claim 1 , ...

TREATING C8- C10 AROMATIC FEED STREAMS TO PREPARE AND RECOVER TRIMETHYLATED BENZENES

Methods are provided for the treatment of a feed stream containing C9 aromatic components to produce mesitylene-containing products. The methods include hydrodealkylating the feed stream to remove C2 and higher alkyl groups from the aromatic components and transalkylating the feed stream to rearrange the distribution of methyl groups among the aromatic components. Disclosed methods also include the treatment of a hydrocarbon feedstock by hydrodealkylation and/or transalkylation in order to produce a hydrocarbon product having an increased mass percentage of mesitylene. 1. A method for the production of mesitylene from an aromatic composition comprising aromatic components including methyl benzenes and Cand/or higher alkyl benzenes , comprising:{'sub': '2', 'a. hydrodealkylating the aromatic components to convert the Cand/or higher alkyl benzenes to the corresponding alkanes and dealkylated aromatics while retaining the methyl benzenes;'}b. transalkylating the methyl benzenes to redistribute the methyl groups among the methyl benzenes to form trimethylbenzenes and other methylated benzenes;c. isomerizing the trimethylbenzenes to increase the amount of mesitylene in the aromatic composition; andd. recovering a TMB-rich product from the aromatic composition.2. The method of in which said recovering a TMB-rich product is by distillation.3. The method of in which said hydrodealkylating is performed in the presence of a suitable hydrodealkylating catalyst claim 1 , and the transalkylating is performed in the presence of a suitable transalkylating catalyst.4. The method of and which further includes combining elemental hydrogen with the feed stream for hydrodealkylating.5. The method of which further includes combining one or more of nitrogen claim 4 , methane claim 4 , ethane and propane with the feed stream for hydrodealkylating.6. The method of which includes removing elemental hydrogen claim 1 , methane claim 1 , ethane and propane from the dealkylated product and ...

Liquid Phase Transalkylation Process

Methods and corresponding catalysts are provided for transalkylation of 1-ring (C) aromatic compounds, such as transalkylation to form para-xylene and/or other xylenes. Suitable catalysts include molecular sieves having a 3-D 12-member ring framework structure, molecular sieves having a 1-D 12-member ring framework structure, acidic microporous materials with a pore channel size of at least 6.0 Angstroms, and/or molecular sieves having a MWW framework structure. The methods include performing transalkylation where at least a portion of the feed to the transalkylation process is in the liquid phase. Optionally, the transalkylation conditions can correspond to conditions where a continuous liquid phase is present within the reaction environment. Some embodiments include liquid phase transalkylation processes for naphthalene-containing feedstock streams. 1. A method for liquid phase transalkylation of aromatic compounds , comprising:{'sub': '9+', 'exposing an aromatic feedstock comprising C aromatics and at least one of benzene and toluene to a transalkylation catalyst under effective transalkylation conditions to form a transalkylation effluent;'}wherein the mole fraction of aromatic compounds in the liquid phase in the feedstock, relative to the total amount of aromatic compounds in the feedstock, is at least about 0.01 under the effective transalkylation conditions;{'sub': '8', 'wherein the transalkylation effluent has a higher weight percentage of Caromatics than the feedstock; and'} a molecular sieve with a 3-dimensional 12-member ring or larger pore network;', 'a molecular sieve with a 1-dimensional 12-member ring or larger pore network, wherein the 1-dimensional channel has a pore channel size of at least 6.0 Angstroms;', 'an acidic microporous material with a pore channel size of at least 6.0 Angstroms; and', 'a molecular sieve having a MWW framework., 'wherein the catalyst comprises at least one of the following2. The method of claim 1 , wherein the molecular ...

Catalyst for Converting Alkylaromatic Hydrocarbon and Preparation Method Thereof

Disclosed are a bifunctional catalyst and a preparation method therefor, the bifunctional catalyst being suitable to produce high-value aromatic hydrocarbons by subjecting alkylaromatic hydrocarbons to a disproportionation/transalkylation/dealkylation reaction while suppressing aromatic loss or subjecting C8 aromatic hydrocarbons to an isomerization reaction while suppressing xylene loss. 1. A method for preparing a catalyst for converting aromatic hydrocarbons , the method comprising:a) supporting a precursor of a first metal having hydrogenation activity on a refractory inorganic oxide binder to prepare a first metal precursor-supported binder;b) combining a first zeolite and/or a second zeolite with the first metal precursor-supported binder to prepare a shaped body; andc) calcining the shaped body to form a catalyst, in which the first metal is supported on a mixed support containing the first zeolite and/or the second zeolite and the binder,wherein the first zeolite has a silica-alumina ratio (SAR) of 5 to 300 and a 10-membered ring pore structure, and the second zeolite has a silica-alumina ratio (SAR) of 5 to 300 and a 12-membered ring pore structure with a pore diameter of 6 to 9 Å, andwherein the first metal is selectively supported on the refractory inorganic oxide binder in the mixed support, the amount of the first metal supported being in the range of 0.01 to 5 wt % on the basis of the weight of the mixed support.2. The method of claim 1 , wherein the refractory inorganic oxide is at least one selected from the group consisting of alumina claim 1 , silica claim 1 , aluminum phosphate claim 1 , titania claim 1 , zirconia claim 1 , bentonite claim 1 , kaolin claim 1 , clinoptilolite claim 1 , and montmorillonite.3. The method of claim 1 , wherein the first zeolite is at least one selected from the group consisting of ZSM-5 claim 1 , ZSM-11 claim 1 , ZSM-23 claim 1 , ZSM-48 claim 1 , ZSM-57 claim 1 , EU-2 claim 1 , TNU-9 claim 1 , and MCM-22.4. The method ...

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 , ...

Flexible unit for isomerization and disproportionation of hydrocarbons using solid acid catalysts

A flexible hydrocarbon conversion process utilizing the same reaction zone for isomerization and disproportionation is described. The feed and type of products are selected. The hydrocarbon feed is contacted with a catalyst and in the presence of hydrogen and an added chloride promoter. The catalyst comprises a solid catalyst comprising a refractory inorganic oxide having a metal halide dispersed thereon. The operating conditions are varied depending on whether isomerization or disproportionation is desired.

TREATING C8-C10 AROMATIC FEED STREAMS TO PREPARE AND RECOVER TRANSMETHYLATED BENZENES

Methods are provided for the treatment of a feed stream containing C9 aromatic components to produce mesitylene-containing products. The methods include hydrodealkylating the feed stream to remove C2 and higher alkyl groups from the aromatic components and transalkylating the feed stream to rearrange the distribution of methyl groups among the aromatic components. Disclosed methods also include the treatment of a hydrocarbon feedstock by hydrodealkylation and/or transalkylation in order to produce a hydrocarbon product having an increased mass percentage of mesitylene. 1. A method for the production of mesitylene from an aromatic composition comprising aromatic components including methyl benzenes and Cand/or higher alkyl benzenes , comprising:{'sub': '2', 'a. hydrodealkylating the aromatic components to convert the Cand/or higher alkyl benzenes to the corresponding alkanes and dealkylated aromatics while retaining the methyl benzenes;'}b. transalkylating the methyl benzenes to redistribute the methyl groups among the methyl benzenes to form trimethylbenzenes and other methylated benzenes;c. isomerizing the trimethylbenzenes to increase the amount of mesitylene in the aromatic composition; andd. recovering a TMB-rich product from the aromatic composition.2. The method of in which said recovering a TMB-rich product is by distillation.3. The method of in which said hydrodealkylating is performed in the presence of a suitable hydrodealkylating catalyst claim 1 , and the transalkylating is performed in the presence of a suitable transalkylating catalyst.4. The method of and which further includes combining elemental hydrogen with the feed stream for hydrodealkylating.5. The method of which further includes combining one or more of nitrogen claim 4 , methane claim 4 , ethane and propane with the feed stream for hydrodealkylating.6. The method of which includes removing elemental hydrogen claim 1 , methane claim 1 , ethane and propane from the dealkylated product and ...

METHOD OF HYDROGENOLYSIS FOR IMPROVED PRODUCTION OF PARAXYLENE

The invention relates to a selective hydrogenolysis method for treating a feed rich in aromatic compounds having more than 8 carbon atoms, comprising transforming at least one alkyl group with at least two carbon atoms (ethyl, propyl, butyl, isopropyl, etc.) attached to a benzene ring into at least one methyl group. The invention also relates to the integration of the hydrogenolysis unit into an aromatic complex. 1- A selective hydrogenolysis process in which a feedstock rich in aromatic compounds having more than 8 carbon atoms is treated and which consists in converting one or more alkyl group(s) having at least two carbon atoms (ethyl , propyl , butyl , isopropyl and the like) attached to a benzene nucleus into one or more methyl group(s) , said process being carried out in the presence of a catalyst comprising at least one metal from Group VIII of the Periodic Table , preferably nickel or platinum , and a porous support comprising at least one crystalline or noncrystalline refractory oxide , having or not having structured porosity , the reaction taking place:at a temperature of between 300° C. and 550° C., preferentially of between 350° C. and 500° C., and more preferentially still of between 370° C. and 450° C.,at a pressure of between 1 and 30 bar, preferentially of between 2 and 20 bar, and more preferentially still of between 2 and 10 bar,{'sub': '2', 'with a H/HC molar ratio of between 1 and 10, and preferentially of between 1.5 and 6,'}{'sup': −1', '−1', '−1, 'with an HSV of between 0.1 and 50 h, preferentially between 1 and 30 hand more preferentially still between 3 and 20 h.'}2- The selective hydrogenolysis process as claimed in claim 1 , in which the reactor used in said process is of fixed bed type and the catalyst support is provided in the form of extrudates.3- The selective hydrogenolysis process as claimed in claim 1 , in which the reactor used in said process is of moving bed type and the catalyst support is provided in the form of approximately ...

PROCESS FOR MAKING MODIFIED SMALL-CRYSTAL MORDENITE, TRANSALKYLATION PROCESS USING SAME, AND MODIFIED SMALL-CRYSTAL MORDENITE

A modified UZM-14 zeolite is described. The modified UZM-14 zeolite has a Modification Factor of 6 or more. The modified UZM-14 zeolite may have one or more of: a Si/Alratio of 14 to 30; a total pore volume in a range of 0.5 to 1.0 cc/g; at least 5% of a total pore volume being mesopores having a diameter of 10 nm of less; a cumulative pore volume of micropores and mesopores having a diameter of 100 Å or less of 0.25 cc/g or more; or a Collidine IR Bronsted acid site distribution greater than or equal to an area of 3/mg for a peak in a range of 1575 to 1700 cmafter desorption at 150° C. Processes of making the modified UZM-14 zeolite and transalkylation processes using the modified UZM-14 zeolite are also described. 1. A catalyst suitable for the conversion of aromatic hydrocarbons comprising:a modified UZM-14 zeolite having a Modification Factor of 6 or more, wherein the modified UZM-14 zeolite is an ion exchanged, caustic washed, acid washed UZM-14 zeolite.2. The catalyst of wherein the modified UZM-14 zeolite has a Si/Alratio of 14 to 30.3. The catalyst of wherein the modified UZM-14 zeolite has a total pore volume in a range of 0.5 to 1.0 cc/g.4. The catalyst of wherein the modified UZM-14 zeolite has at least 5% of a total pore volume being mesopores having a diameter of 10 nm of less.5. The catalyst of wherein the modified UZM-14 zeolite has a cumulative pore volume of micropores and mesopores having a diameter of 100 Å or less of 0.25 cc/g or more.6. The catalyst of wherein the modified UZM-14 zeolite has a Collidine IR Bronsted acid site distribution greater than or equal to an area of 3/mg for a peak in a range of 1575 to 1700 cm-1 after desorption at 150° C.7. The catalyst of wherein the catalyst further comprises an additional zeolitic component selected from one or more of MFI claim 1 , MEL claim 1 , EUO claim 1 , FER claim 1 , MFS claim 1 , MTT claim 1 , MTW claim 1 , TON and FAU.8. The catalyst of wherein the catalyst further comprises a binder ...

Combined heavy reformate dealkylation-transalkylation process for maximizing xylenes production

The present invention relates to a method of forming mixed xylenes from a heavy reformate using a dealkylation-transalkylation system that includes the step of introducing a heavy reformate containing methyl ethyl benzenes and tri-methyl benzenes and sufficiently free of toluene into the dealkylation stage with a hydrogen-containing material such that the heavy reformate and the hydrogen-containing material intermingle and contact a hydrodealkylation catalyst. The dealkylation-transalkylation system includes dealkylation stages, non-aromatic product gas separations and transalkylation stages. The BTEX component toluene forms from the reaction of methyl ethyl benzenes and hydrogen in the presence of the hydrodealkylation catalyst. The method also includes the step of introducing a dealkylated heavy reformate into the transalkylation stage such that the dealkylated heavy reformate contacts a transalkylation catalyst, forming a transalkylation stage product mixture that includes mixed xylenes.

Heavy Aromatics Conversion Processes and Catalyst Compositions Used Therein

Disclosed are processes for conversion of a feedstock comprising C aromatic hydrocarbons to lighter aromatic products in which the feedstock and optionally hydrogen are contacted in the presence of the catalyst composition under conversion conditions effective to dealkylate and transalkylate said C aromatic hydrocarbons to produce said lighter aromatic products comprising benzene, toluene and xylene. The catalyst composition comprises a zeolite, a first metal, and a second metal, and is treated with a source of sulfur and/or a source of steam. 125.-. (canceled)26. A catalyst composition comprising (i) one or more zeolites selected from zeolite beta , ZSM-5 , ZSM-12 and mordenite zeolites synthesized from TEA or MTEA , said mordenite zeolites having a mesopore surface area of greater than 30 m/g and said mordenite zeolites comprising agglomerates composed of primary crystallites , wherein said primary crystallites have an average primary crystal size as measured by TEM of less than 80 nm and an aspect ratio of less than 2 , (ii) 0.001 wt. % to 20.0 wt. % of at least one first metal comprising molybdenum or tungsten , based on the weight of the catalyst composition , and (iii) 0.001 wt. % to 20.0 wt. % of at least one second metal comprising cobalt or nickel , based on the weight of the catalyst composition ,wherein said catalyst composition is treated with a source of sulfur in one or more steps at temperatures in the range 204° C. (400° F.) up to about 480° C. (900° F.) or treated with a source of steam which comprises up to about 100% steam at temperatures in the range of about 260° C. (500° F.) to about 649° C. (1200° F.).27. The catalyst composition of claim 26 , wherein said source of sulfur is one or more of hydrogen sulfide claim 26 , carbon disulfide and alkylsulfides which are selected from the group consisting of methylsulfide claim 26 , dimethylsulfide claim 26 , dimethyldisulfide claim 26 , diethylsulfide and dibutyl sulfide claim 26 , and mixtures of two ...

Transalkylation Process

Disclosed is a transalkylation process for making an aromatic material between a light aromatic material and a heavier aromatic material in the presence of hydrogen and a transalkylation catalyst comprising a hydrogenation component and a transalkylation component. The process comprises conducting the transalkylation reaction under conditions conducive to reducing the amount of cyclic compounds in the transalkylation reaction mixture in the beginning phase of the operation that is different from the conditions after the beginning phase. The invention is useful, e.g., in transalkylation between toluene and C9+ aromatic feed materials to produce xylenes and/or benzene.

UZM-54 AND TRANSALKYLATION PROCESS USING SAME

A catalyst suitable for the conversion of aromatic hydrocarbons is described. The catalyst comprises UZM-54 zeolite; a mordenite zeolite; a binder comprising alumina, silica, or combinations, thereof; and a metal selected from one or more of: Groups VIB(6) VIIB(7), VIII(8-10) and IVA(14) of the Periodic Table. A process for transalkylation using the catalyst is also described. 1. A catalyst suitable for the conversion of aromatic hydrocarbons comprising:UZM-54 zeolite;a mordenite zeolite;a binder comprising alumina, silica, or combinations, thereof; anda metal selected from one or more of: Groups VIB(6) VIIB(7), VIII(8-10) and IVA(14) of the Periodic Table.2. The catalyst of wherein the catalyst comprises about 20 to about 60 wt % of the UZM-54 zeolite claim 1 , about 20 to about 60 wt % of the mordenite zeolite claim 1 , about 10 to about 40 wt % of the binder claim 1 , and about 0.1 to about 10 wt % of the metal.3. The catalyst of wherein the UZM-54 zeolite has less than about 500 wppm Na.4. The catalyst of wherein the binder comprises alumina.5. The catalyst of wherein the metal comprises one or more of: Mo claim 1 , Ni claim 1 , Re claim 1 , Pt claim 1 , or Pd.6. The catalyst of wherein the catalyst comprisesabout 20 to about 60 wt % of the UZM-54 zeolite;about 20 to about 60 wt % of the mordenite zeolite;about 10 to about 40 wt % of the binder; and,about 0.1 to about 10 wt % of the metal wherein the metal comprises one or more of: Mo, Ni, Re, Pt, or Pd.7. The catalyst of wherein the UZM-54 zeolite has less than about 500 wppm Na.8. The catalyst of wherein the binder comprises alumina.9. A process for transalkylation of a feedstream comprising one or more of C claim 6 , C claim 6 , Cand C aromatics to obtain a transalkylation product stream having an increased concentration of Caromatics relative to that of the feedstream claim 6 , comprising contacting the feedstream at transalkylation conditions with a catalyst comprising:UZM-54 zeolite;a mordenite zeolite;a ...

Catalyst Compositions and Their Use in Aromatic Alkylation Processes

Catalyst composition which comprises a first zeolite having a BEA* framework type and a second zeolite having a MOR framework type and a mesopore surface area of greater than 30 m/g is disclosed. These catalyst compositions are used to remove catalyst poisons from untreated feed streams having one or more impurities which cause deactivation of the downstream catalysts employed in hydrocarbon conversion processes, such as those that produce mono-alkylated aromatic compounds. 1. A catalyst composition comprising a first zeolite having a BEA* framework type and a second zeolite having a MOR framework type and a mesopore surface area of greater than 30 m/g as measured by BET.2. The catalyst composition of claim 1 , wherein said first zeolite is zeolite beta.3. The catalyst composition of claim 1 , wherein said second zeolite is EMM-34.4. The catalyst composition of claim 3 , wherein said second zeolite comprising agglomerates of primary crystallites claim 3 , wherein said primary crystallites have an average primary crystal size of less than 80 nm in each of the a claim 3 , b and c crystal vectors as measured by X-ray diffraction and an aspect ratio of less than 2 claim 3 , wherein the aspect ratio is defined as the longest dimension of the crystallite divided by the width of the crystallite claim 3 , wherein said width of the crystallite is defined as the dimension of the crystallite in the middle of that longest dimension in a direction orthogonal to that longest dimension claim 3 , as measured by TEM.5. The catalyst composition of claim 4 , wherein said EMM-34 has a ratio of the mesopore surface area to the total surface area of greater than 0.05.6. The catalyst composition of claim 5 , wherein said second zeolite is synthesized from TEA or MTEA.7. The catalyst composition of claim 6 , wherein the Si/Almolar ratio of said second zeolite is in the range of 10 to 60.8. The catalyst composition claim 7 , wherein said catalyst composition has a collidine uptake in the ...

Process for Producing Cyclohexylbenzene

In a process for producing cyclohexylbenzene, benzene is reacted with cyclohexene under alkylation conditions effective to produce an alkylation effluent comprising cyclohexylbenzene and a polycyclohexylbenzene. A first feed comprising at least a portion of the alkylation effluent is then fed to a first separation device, where the first feed is separated into at least a first fraction containing cyclohexylbenzene and a second fraction containing the polycyclohexylbenzene, the second fraction also comprising an oxygenated hydrocarbon. At least a portion of the oxygenated hydrocarbon is removed from at least a portion of the second fraction in a second separation device to obtain a second feed. The second feed may then be reacted in a transalkylation or dealkylation reactor to convert at least part of the polycyclohexylbenzene to additional cyclohexylbenzene.

PROCESS FOR MAXIMIZING PRODUCTION OF XYLENES FROM HEAVY REFORMATE WITHOUT PURGE

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit. 1. A method for producing mixed xylenes from a heavy reformate feed , the method comprising the steps of:introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst, wherein the heavy reformate feed comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas;reacting the heavy reformate feed with the hydrogen feed in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, wherein the dealkylation reactor is at a dealkylation temperature, wherein the dealkylation reactor is at a dealkylation pressure, wherein the dealkylation reactor has a liquid hourly space velocity;introducing the dealkylation effluent to a splitter unit, where the dealkylation effluent comprises light gases, toluene, benzene, mixed xylenes, and C9+ aromatics;separating the dealkylation effluent into a light gas stream, a toluene stream, a ...

Dealkylation and Transalkylation of Heavy Aromatic Hydrocarbons

A process for producing xylene from Caromatic hydrocarbons comprises contacting a first feedstock comprising Caromatic hydrocarbons with a first catalyst in the presence of hydrogen under effective vapor phase dealkylation conditions to dealkylate part of the Caromatic hydrocarbons and produce a first product comprising benzene and unreacted Caromatic hydrocarbons. A second feedstock comprising toluene is contacted with a second catalyst in the presence of hydrogen under effective vapor phase toluene disproportionation conditions to disproportionate at least part of the toluene and produce a second product comprising para-xylene. A third feedstock comprising Caromatic hydrocarbons and benzene and/or toluene is contacted with a third catalyst in the presence of hydrogen under effective liquid phase Ctransalkylation conditions to transalkylate at least part of the Caromatic hydrocarbons and produce a third product comprising xylenes. 1. A process for producing xylene from Caromatic hydrocarbons , the process comprising:{'sub': 9+', '9+', '9+, '(a) contacting a first feedstock comprising Caromatic hydrocarbons with a first catalyst in the presence of 0 wt. % or more of hydrogen under effective vapor phase dealkylation conditions to dealkylate part of the Caromatic hydrocarbons and produce a first product comprising benzene and unreacted Caromatic hydrocarbons;'}(b) contacting a second feedstock comprising toluene with a second catalyst in the presence of hydrogen under effective vapor phase toluene disproportionation conditions to disproportionate at least part of the toluene and produce a second product comprising para-xylene; and{'sub': 9+', '9+, '(c) contacting a third feedstock comprising C9+ aromatic hydrocarbons and benzene and/or toluene with a third catalyst in the presence of hydrogen under effective liquid phase Ctransalkylation conditions to transalkylate at least part of the Caromatic hydrocarbons and produce a third product comprising xylenes.'}2. The ...

Process for Preparing a Molecular Sieve

The present invention provides a mordenite zeolite having a mesopore surface area of greater than 30 m 2 /g and an average primary crystal size as measured by TEM of less than 80 nm, and methods of making the mordenite zeolite.

Transalkylation of Heavy Aromatic Hydrocarbon Feedstocks

A process for producing xylene comprises contacting a first feed comprising C 9+ aromatic hydrocarbons and hydrogen with a first catalyst composition comprising a first molecular sieve having a Constraint Index of 3 to 12 and at least one hydrogenation component. The first catalyst composition dealkylates at least part of the C 9+ aromatic hydrocarbons containing C 2+ alkyl groups and to saturate the resulting C 2+ olefins to produce a second feed. The second feed is then contacted with a second catalyst composition under conditions effective to transalkylate at least part of the C 9+ aromatic hydrocarbons in the second feed to produce a product comprising xylene. The second catalyst composition comprises a second molecular sieve having a Constraint Index less than 3 and a third molecular sieve having a Constraint Index of 3 to 12.

TOLUENE DISPROPORTIONATION USING AN ENHANCED UZM-39 ALUMINOSILICATE ZEOLITE

Toluene disproportionation processes utilizing treated UZM-39 zeolites are described. The processes produce effluent streams comprising para-xylene and benzene. The molar ratio of benzene to xylene (Bz/X) in the effluent stream can be in a range of about 1.00 to about 1.14, the molar ratio of para-xylene to xylene (pX/X) in the effluent stream can be in a range of about 0.80 to about 1.0, and the conversion of toluene can be about 20% to about 40%. 1. A toluene disproportionation process comprising contacting a feed comprising toluene with a catalyst comprising a microporous crystalline zeolite at disproportionation conditions to produce an effluent stream comprising para-xylene and benzene , wherein a molar ratio of benzene to xylene in the effluent stream is in a range of about 1.00 to about 1.14 , wherein a molar ratio of para-xylene to xylene in the effluent stream is in a range of about 0.80 to about 1.0 , and wherein a conversion of toluene is about 20% to about 40%; andwherein the zeolite has been enhanced with at least one enhancement selected from treatment for deposition of carbon, treatment for deposition of silica, or both.2. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08.4. (canceled)5. The process of wherein the at least one enhancement treatment step comprises at least one treatment to incorporate silica.6. The process of wherein the catalyst is steamed after the at least one enhancement treatment step.7. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08 and wherein the range of the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.95.8. The process of wherein a selectivity to xylenes is greater than 52% when the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.90.9. The process of wherein a selectivity to light ends is less than about 3.5% when the molar ratio of para-xylene to xylene ...

TOLUENE DISPROPORTIONATION USING AN ENHANCED UZM-44 ALUMINOSILICATE ZEOLITE

Toluene disproportionation processes utilizing treated UZM-44 zeolites are described. The processes produce effluent streams comprising para-xylene and benzene. The molar ratio of benzene to xylene (Bz/X) in the effluent stream can be in a range of about 1.00 to about 1.14, the molar ratio of para-xylene to xylene (pX/X) in the effluent stream can be in a range of about 0.80 to about 1.0, and the conversion of toluene can be about 20% to about 40%. 1. A toluene disproportionation process comprising contacting a feed comprising toluene with a catalyst comprising a microporous crystalline zeolite at disproportionation conditions to produce an effluent stream comprising para-xylene and benzene , wherein the zeolite is UZM-44 , wherein a molar ratio of benzene to xylene in the effluent stream is in a range of about 1.00 to about 1.14 , wherein a molar ratio of para-xylene to xylene in the effluent stream is in a range of about 0.80 to about 1.0 , wherein a conversion of toluene is about 20% to about 40%; andwherein the catalyst has been enhanced with at least one enhancement treatment step selected from treatment for deposition of carbon, treatment for deposition of silica, or both.2. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08.4. (canceled)5. The process of wherein the at least one enhancement treatment step comprises at least one treatment to incorporate silica.6. The process of wherein the catalyst is steamed after the at least one enhancement treatment step.7. The process of wherein the molar ratio of benzene to xylene is in the range of about 1.00 to about 1.08 and wherein the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.95.8. The process of wherein a selectivity to xylenes is greater than 52% when the molar ratio of para-xylene to xylene is in the range of about 0.80 to about 0.90.9. The process of wherein a selectivity to light ends is less than about 3.5% when the molar ...

Aromatic Compositions and Methods for Obtaining Them

Aromatic compositions useful in various applications, such as aromatic fluid solvents and high temperature heat transfer fluids, are provided herein. Also provided are advantageous methods for obtaining the aromatic compositions, utilizing hydroalkylation of precursor aromatic hydrocarbons such as benzene, toluene, xylene, and the like. Particularly preferred aromatic compositions include one or more of cycloalkylaromatic, dicycloalkylaromatic, biphenyl, terphenyl, and diphenyl oxide compounds. The aromatic compositions may be blended with an aromatic solvent or other aromatic fluid comprising one or more of alkylnaphthalenes, alkylbenzenes, and naphthalene, e.g., to form a useful aromatic fluid solvent, or the aromatic compositions may be utilized as high temperature heat transfer fluids (with or without additional blend components). 1. A process comprising:(a) obtaining a first aromatic composition from one or more precursor aromatic hydrocarbons, wherein the first aromatic composition comprises one or more of: (i) one or more cycloalkylaromatic compounds; (ii) one or more dicycloalkylaromatic compounds; (iii) one or more biphenyl compounds; and (iv) one or more terphenyl compounds; wherein obtaining the first aromatic composition comprises one of:', '(a-1) contacting a hydroalkylation feed comprising the one or more aromatic hydrocarbons with hydrogen in the presence of a hydroalkylation catalyst so as to produce a hydroalkylation reaction effluent comprising (i) the one or more cycloalkylaromatic compounds and (ii) the one or more dicycloalkylaromatic compounds; and', '(a-2) contacting a transalkylation feed comprising the one or more aromatic hydrocarbons with a precursor cycloalkylaromatic compound in the presence of a transalkylation catalyst so as to produce a transalkylation reaction effluent comprising the one or more cycloalkylaromatic compounds and the one or more dicycloalkylaromatic compounds., '(b) blending the first aromatic composition with a second ...

SYSTEMS AND PROCESSES FOR DIRECT CRUDE OIL UPGRADING TO HYDROGEN AND CHEMICALS

Systems and methods for direct crude oil upgrading to hydrogen and chemicals including separating an inlet hydrocarbon stream into a light fraction and a heavy fraction comprising diesel boiling point temperature range material; producing from the light fraction syngas comprising Hand CO; reacting the CO produced; producing from the heavy fraction and separating CO, polymer grade ethylene, polymer grade propylene, Ccompounds, cracking products, light cycle oils, and heavy cycle oils; collecting and purifying the COproduced from the heavy fraction; processing the Ccompounds to produce olefinic oligomerate and paraffinic raffinate; separating the cracking products; oligomerizing a light cut naphtha stream; hydrotreating an aromatic stream; hydrocracking the light cycle oils to produce a monoaromatics product stream; gasifying the heavy cycle oils; reacting the CO produced from gasifying the heavy cycle oils; collecting and purifying the CO; and processing and separating produced aromatic compounds into benzene and para-xylene. 1. A method for hydrocarbon separation and upgrading , the method comprising the steps of:separating an inlet hydrocarbon stream into a light fraction comprising naphtha boiling point temperature range material and a heavy fraction comprising diesel boiling point temperature range material;{'sub': '2', 'producing from the light fraction syngas comprising Hand CO;'}reacting the CO produced from the light fraction via at least one reaction selected from the group consisting of: carbonylation, polymerization, and water-gas shift;{'sub': 2', '4, 'producing from the heavy fraction and separating CO, polymer grade ethylene, polymer grade propylene, Ccompounds, cracking products comprising naphtha boiling point temperature range products with olefins and aromatics, light cycle oils, and heavy cycle oils;'}{'sub': '2', 'collecting and purifying the COproduced from the heavy fraction;'}{'sub': '4', 'processing the Ccompounds to produce olefinic ...

Rhenium Promoted Catalyst

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

PROCESS FOR XYLENE PRODUCTION WITH ENERGY OPTIMIZATION

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit. 1. A system for producing mixed xylenes from a heavy reformate feed , the system comprising:a feed exchanger, the feed exchanger configured to transfer heat from a mixed xylene stream to the heavy reformate feed to increase a temperature of the heavy reformate feed to produce a hot feed stream, wherein the feed exchanger is a cross process exchanger, wherein the heavy reformate comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas, wherein a temperature of the mixed xylene stream is reduced to produce a cooled mixed stream;a mixing point fluidly connected to the feed exchanger, the mixing point configured to mix the hot feed stream and a hydrogen feed to produce a mixed feed;a feed-effluent exchanger fluidly connected to the mixing point, the feed-effluent exchanger configured to transfer heat from a dealkylation effluent to the mixed feed to increase a temperature of the mixed feed to produce a hot mixed feed, wherein the feed-effluent exchanger ...

Zeolite composite catalysts for conversion of heavy reformate to xylenes

Embodiments of zeolite composite catalysts and methods of producing the zeolite composite catalysts are provided, where the methods comprise dissolving in an alkaline solution a catalyst precursor comprising at least one mesoporous zeolite while heating, stirring, or both to yield a dissolved zeolite solution, where the mesoporous zeolite has a molar ratio of SiO 2 /Al 2 O 3 of at least 30, where the mesoporous zeolite comprises zeolite beta, adjusting the pH of the dissolved zeolite solution, aging the pH adjusted dissolved zeolite solution to yield solid zeolite composite from the dissolved zeolite solution, and calcining the solid zeolite composite to produce the zeolite composite catalyst, where the zeolite composite catalyst has a mesostructure comprising at least one disordered mesophase and at least one ordered mesophase, and where the zeolite composite catalyst has a surface area defined by the Brunauer-Emmett-Teller (BET) analysis of at least 600 m 2 /g.

Process for Preparing a Molecular Sieve

The present invention provides a mordenite zeolite having a mesopore surface area of greater than 30 m/g and an average primary crystal size as measured by TEM of less than 80 nm, and methods of making the mordenite zeolite. 114.-. (canceled)15. A process for converting a feedstock comprising an organic compound to a conversion product which comprises the step of contacting said feedstock at organic compound conversion conditions with a catalyst comprising a mordenite zeolite , the mordenite zeolite comprising a structure directing agent (SDA) selected from the group consisting of TEA , MTEA and mixtures thereof within its pores , having a mesopore surface area of greater than 30 m/g and comprising agglomerates composed of primary crystallites , wherein the primary crystallites have an average primary crystal size as measured by TEM of less than 80 nm.16. The process of claim 15 , wherein the primary crystallites have an average primary crystal size of less than 80 nm in each of the a claim 15 , b and c crystal vectors as measured by X-ray diffraction.17. The process of claim 15 , wherein at least 90% by number of the primary crystallites have a primary crystal size of less than 80 nm as measured by TEM.18. The process of claim 15 , wherein said primary crystallites have an aspect ratio of less than 2 claim 15 , wherein the aspect ratio is defined as the longest dimension of the crystallite divided by the width of the crystallite claim 15 , where the width of the crystallite is defined as the dimension of the crystallite in the middle of that longest dimension in a dimension orthogonal to that longest dimension claim 15 , as measured by TEM.19. The process of claim 15 , wherein the mordenite zeolite has a mesopore surface area of greater than 40 m/g.20. The process of claim 15 , wherein the ratio of mesopore surface area to the total surface area is greater than 0.05.21. The process of claim 15 , wherein the mordenite zeolite is a calcined mordenite zeolite prepared ...

PROCESSES AND APPARATUSES FOR TOLUENE METHYLATION IN AN AROMATICS COMPLEX

This present disclosure relates to processes and apparatuses for toluene methylation in an aromatics complex for producing paraxylene. More specifically, the present disclosure relates to processes and apparatuses wherein a toluene methylation zone is integrated within an aromatics complex for producing paraxylene thus allowing no benzene byproduct to be produced. This may be accomplished by incorporating a toluene methylation process into the aromatics complex and recycling the benzene to the transalkylation unit the aromatics complex. 1. A process for producing paraxylene with no benzene byproduct , comprising:{'sub': 9', '10, 'a) passing a lighter aromatic stream containing benzene and a heavier aromatic stream containing C-Caromatic compounds to a transalkylation zone;'}{'sub': '8', 'b) subjecting the lighter aromatic stream and the heavier aromatic stream in the transalkylation zone to transalkylation conditions including the presence of a first catalyst to provide a transalkylation product stream having a greater concentration of toluene to Caromatics;'}{'sub': 8', '9+, 'c) separating by fractionation from the transalkylation product stream a first boiling fraction comprising benzene, a second boiling fraction comprising toluene, a third boiling fraction comprising Caromatics and a fourth boiling fraction comprising Caromatics;'}d) recycling at least a portion of the benzene from the transalkylation product stream back to the transalkylation zone;e) passing at least a portion of the second boiling fraction from steps c, g and i and a methanol stream to a toluene methylation zone operating under toluene methylation conditions to produce a toluene methylation product stream;f) separating by fractionation from the toluene methylation product stream the same fractions described in step c;{'sub': 8', '8, 'g) subjecting at least a portion of the third boiling fraction comprising Caromatics of steps c, g and i to a separation zone to selectively remove a para-xylene ...

PROCESSES AND APPARATUSES FOR OLEFIN SATURATION IN AN AROMATICS COMPLEX

Process and apparatuses for producing benzene and para-xylene from a reformate stream is provided. The process comprises separating the reformate stream to provide a first stream comprising Cand lighter hydrocarbons and a second stream comprising aromatic hydrocarbons. The second steam is provided to a reformate splitter to provide a reformate bottoms stream comprising C aromatic hydrocarbons and a reformate overhead stream comprising C aromatic hydrocarbons. The reformate overhead stream is passed to an aromatics extraction unit to provide an aromatics extract stream comprising benzene and toluene and a raffinate stream comprising non-aromatic hydrocarbons. The reformate bottoms stream and one of the first stream and the raffinate stream is passed to an olefin reduction zone, wherein the reformate bottoms stream and one of the first stream and the raffinate stream are contacted with an olefin saturation catalyst under olefin saturation conditions to produce an olefin-treated reformate stream. 1. A process for producing benzene and para-xylene from a reformate stream , wherein the process comprises:{'sub': '4', 'a) separating the reformate stream to provide a first stream comprising Cand lighter hydrocarbons and a second stream comprising aromatic hydrocarbons;'}{'sub': 8+', '7−, 'b) providing the second steam to a reformate splitter to provide a reformate bottoms stream comprising C aromatic hydrocarbons and a reformate overhead stream comprising C aromatic hydrocarbons;'}c) passing the reformate overhead stream to an aromatics extraction unit to provide an aromatics extract stream comprising benzene and toluene and a raffinate stream comprising non-aromatic hydrocarbons; andd) passing the reformate bottoms stream and one of the first stream and the raffinate stream to an olefin reduction zone, wherein the reformate bottoms stream and one of the first stream and the raffinate stream are contacted with an olefin saturation catalyst under olefin saturation conditions ...

METHODS OF HEAVY REFORMATE CONVERSION INTO AROMATIC COMPOUNDS

Method of making BTX compounds including benzene, toluene, and xylene, including feeding heavy reformate to a reactor containing a composite zeolite catalyst. The composite zeolite catalyst includes a mixture of layered mordenite (MOR-L) comprising a layered or rod-type morphology with a layer thickness less than 30 nm and ZSM-5. The MOR-L, the ZSM-5, or both include one or more impregnated metals. The method further includes producing the BTX compounds by simultaneously performing transalkylation and dealkylation of the heavy reformate in the reactor. The composite zeolite catalyst is able to simultaneously catalyze both the transalkylation and dealkylation reactions. 1. A composite zeolite catalyst ,the composite zeolite catalyst comprising a mixture of layered mordenite (MOR-L) and ZSM-5, where:the MOR-L or both the MOR-L and ZSM-5 comprise one or more impregnated metals,the MOR-L comprises a rod morphology with a smallest dimension less than 28 nm,{'sup': '2', 'the MOR-L without the impregnated metals comprises an external surface area greater than 120 m/g, and'}the MOR-L has a molar ratio of silicon to aluminum (Si/Al) from 4:1 to 8:1.2. The composite zeolite catalyst of claim 1 , where the one or more impregnated metals are selected from the group consisting of molybdenum claim 1 , chromium claim 1 , platinum claim 1 , nickel claim 1 , tungsten claim 1 , palladium claim 1 , ruthenium claim 1 , gold claim 1 , rhenium claim 1 , rhodium claim 1 , or combinations thereof and their respective oxides.3. The composite zeolite catalyst of claim 1 , where the one or more impregnated metals comprises rhenium.4. The composite zeolite catalyst of claim 1 , where the MOR-L claim 1 , the ZSM-5 claim 1 , or both the MOR-L and ZSM-5 comprise up to 20 wt. % of the one or more impregnated metals.5. The composite zeolite catalyst of claim 1 , where the MOR-L is impregnated with 0.25 to 0.5 wt. % rhenium.6. The composite zeolite catalyst of claim 1 , where the ZSM-5 is ...

Aromatics Production Process

In a process for producing para-xylene, at least one feed comprising C aromatic hydrocarbons is supplied to a dividing wall distillation column to separate the feed into a C aromatic hydrocarbon-containing stream, a Caromatic hydrocarbon-containing stream and a C aromatic hydrocarbon-containing stream. At least part of the Caromatic hydrocarbon-containing stream is then supplied to a para-xylene recovery unit to recover para-xylene from the Caromatic hydrocarbon-containing stream and produce a para-xylene depleted stream. The para-xylene depleted stream is contacted with a xylene isomerization catalyst in a xylene isomerization zone under conditions effective to isomerize xylenes in the para-xylene depleted stream and produce an isomerized stream, which is then at least partially recycled to the para-xylene recovery unit. 1. A process for producing para-xylene and benzene , the process comprising:{'sub': 6+', '7−', '8', '9+, '(a2) supplying a feed comprising a mixture of C aliphatic and aromatic hydrocarbons to a dividing wall distillation column to separate the feed into a C hydrocarbon-containing stream, a Chydrocarbon-containing stream and a C hydrocarbon-containing stream;'}{'sub': 7−', '7−, '(b2) removing at least part of the aliphatic hydrocarbons from the C hydrocarbon-containing stream to produce a C aromatic hydrocarbon-enriched stream;'}{'sub': 7−', '7−, '(c2) supplying at least part of the C aromatic-enriched stream to a separation unit to separate the C aromatic-enriched stream into a benzene-containing stream and a toluene-containing stream;'}{'sub': 8', '8, '(d2) supplying at least part of the Chydrocarbon-containing stream to a para-xylene recovery unit to recover para-xylene from the Chydrocarbon-containing stream and produce apara-xylene depleted stream;'}(e2) contacting at least part of the para-xylene depleted stream with a xylene isomerization catalyst in a xylene isomerization zone under conditions effective to isomerize xylenes in the para- ...

PROCESSES FOR INCREASING THE OVERALL AROMATICS AND XYLENES YIELD IN AN AROMATICS COMPLEX

The present subject matter describes processes for increasing overall aromatics and xylenes yield in an aromatics complex. More specifically, the process for increasing overall aromatics and xylenes yield in an aromatics complex accomplishes the increased yields by incorporating an A-Aisomerization step into the aromatics complex. This isomerization integration increases the para-xylene. 1. A process for increasing overall xylenes yield in an aromatics complex , the process comprising the steps of:{'sub': 7', '8', '10', '10, 'separating an aromatics-rich reformate into a first hydrocarbon stream comprising C− hydrocarbons, a second hydrocarbon stream comprising C-Caromatics, and a third hydrocarbon stream comprising C+ aromatics;'}{'sub': 8', '10', '8', '10, 'isomerizing the second hydrocarbon stream comprising C-Caromatics to produce a C-Cisomerization product stream;'}{'sub': 8', '10, 'passing the C-Cisomerization product stream to a napthene dehydrogenation zone to produce a napthene dehydrogenation zone product stream;'}{'sub': 7', '8, 'separating the napthene dehydrogenation zone product stream into a first napthene dehydrogenation zone product stream comprising C− hydrocarbons and a second naphthene dehydrogenation zone product stream comprising C+ aromatics; and'}{'sub': '8', 'passing the second napthene dehydrogenation zone product stream comprising C+ aromatics to a xylenes recovery section or transalkylation zone.'}2. The process of claim 1 , wherein the step of isomerizing comprises using an isomerization catalyst comprising a 12-member ring zeolite or 10-member ring zeolite claim 1 , a binder claim 1 , and a platinum-group metal component.3. The process of claim 1 , wherein the step of isomerizing comprises a temperature range of about 250° C. to about 450° C.4. The process of claim 1 , wherein the step of isomerizing comprises a pressure range of about 3 bar to about 15 bar.5. The process of claim 1 , wherein the napthene dehydrogenation zone comprises ...

Process of Producing Cyclohexylbenzene

In a process for producing cyclohexylbenzene, benzene is contacted with hydrogen under hydroalkylation conditions effective to form a first effluent stream comprising cyclohexylbenzene, cyclohexane, methylcyclopentane, and unreacted benzene. At least a portion of the first effluent stream is contacted with a dehydrogenation catalyst under dehydrogenation conditions to convert at least a portion of the cyclohexane to benzene thereby forming a second effluent stream. The amount of methylcyclopentane in the second effluent stream is different by no more than 65% of the total amount of the portion of the first effluent stream, said amounts being on a weight basis. A methylcyclopentane-containing stream is removed from either the first or the second effluent stream and at least a portion of the second effluent stream containing benzene is recycled to the hydroalkylation step.

Methods of producing composite zeolite catalysts for heavy reformate conversion into xylenes

A method of forming a composite zeolite catalyst includes combining a silicon source and an aqueous organic structure directing agent having a polyamino cation compound to form a silica intermediary gel, introducing an aluminum precursor to the silica intermediary gel to form a catalyst precursor gel, evaporating water in the catalyst precursor gel to form a catalyst gel, and heating the catalyst gel to form a composite zeolite catalyst particle having an intergrowth region with a mixture of both Beta crystals and ZSM-5 crystals. An associated method of making xylene includes feeding heavy reformate to a reactor, the reactor containing the composite zeolite catalyst, and producing xylene by simultaneously performing dealkylation and transalkylation of the heavy reformate in the reactor, where each composite zeolite catalyst particle is able to catalyze both the dealkylation and transalkylation reactions.

METHODS OF PRODUCING COMPOSITE ZEOLITE CATALYSTS FOR HEAVY REFORMATE CONVERSION INTO XYLENES

A method of forming composite zeolite catalyst particles includes combining a silicon source, an aqueous organic structure directing agent having a polyquaternary ammonium compound, water and an aluminum source to form a catalyst gel. The method also includes heating the catalyst gel to form the composite zeolite catalyst particle having an intergrowth region with a mixture of both Mordenite crystals and ZSM-5 crystals. An associated method of making xylene includes feeding heavy reformate to a reactor, the reactor containing the composite zeolite catalyst particles, and producing xylene by simultaneously performing dealkylation and transalkylation of the heavy reformate in the reactor, where each composite zeolite catalyst particle is able to catalyze both the dealkylation and transalkylation reactions. 2. The method of where the silicon source comprises a silica gel claim 1 , silicon oxide claim 1 , silicon halide claim 1 , tetraalkyl orthosilicate claim 1 , silicic acid claim 1 , fumed silica claim 1 , sodium silicate claim 1 , colloidal silica claim 1 , or combinations thereof.3. The method of where the silicon source is a silica gel and the silica gel is a 20 to 60 wt. % suspension of silica in water.4. The method of where the polyquaternary ammonium compound is a diquaternary ammonium compound.5. The method of where claim 1 ,X is a halogen selected from Cl, Br, I, or combinations thereof,{'sub': '18-22', 'R1 is a substituted or an unsubstituted Calkyl group;'}{'sub': '6', 'R2 is a substituted or an unsubstituted Calkyl group; and'}{'sub': '6-8', 'R3 is a substituted or an unsubstituted Calkyl group or an alkenyl group.'}6. The method of where the aluminum source comprises NaAlO.7. The method of where the aluminum source claim 1 , the silicon source claim 1 , the organic structure directing agent claim 1 , and the water are further combined with NaOH to form the catalyst gel.8. The method of where the heating of the catalyst gel is conducted in a sealed vessel ...

Methods of heavy reformate conversion into aromatic compounds

Method of making BTX compounds including benzene, toluene, and xylene, including feeding heavy reformats to a reactor containing a composite zeolite catalyst. The composite zeolite catalyst includes a mixture of nanocrystalline Beta zeolite (Nano-Beta) comprising crystal size in the range of 10 to 40 nm and ZSM-5. The Nano-Beta, the ZSM-5, or both include one or more impregnated metals. The method further includes producing the BTX compounds by simultaneously performing transalkylation and dealkylation of the heavy reformate in the reactor. The composite zeolite catalyst is able to simultaneously catalyze both the transalkylation and dealkylation reactions.

Methods of heavy reformate conversion into aromatic compounds

Method of making BTX compounds including benzene, toluene, and xylene, including feeding heavy reformate to a reactor containing a composite zeolite catalyst. The composite zeolite catalyst includes a mixture of layered mordenite (MOR-L) comprising a layered or rod-type morphology with a layer thickness less than 30 nm and ZSM-5. The MOR-L, the ZSM-5, or both include one or more impregnated metals. The method further includes producing the BTX compounds by simultaneously performing transalkylation and dealkylation of the heavy reformate in the reactor. The composite zeolite catalyst is able to simultaneously catalyze both the transalkylation and dealkylation reactions.

CATALYST FOR CONVERTING HEAVY REFORMATE TO PRODUCE BTX COMPOUNDS

A method of making BTX (benzene, toluene, xylene) compounds by feeding a heavy reformate stream to a reactor, where the reactor includes a composite zeolite catalyst, that contains a mixture of a desilicated mesoporous mordenite and ZSM-5, and in which the desilicated mesoporous mordenite, the ZSM-5, or both, comprise one or more impregnated metals. The composite zeolite catalyst is able to catalyze the transalkylation reaction and the dealkylation reaction simultaneously to produce the BTX compounds. 1. A method of making BTX compounds comprising benzene , toluene , and xylene , the method comprising: where the composite zeolite catalyst comprises a mixture of a desilicated mesoporous mordenite and ZSM-5, and', 'the desilicated mesoporous mordenite, the ZSM-5, or both, comprise one or more impregnated metals; and, 'feeding a heavy reformate stream to a reactor, the reactor comprising a composite zeolite catalyst,'}producing the BTX compounds by simultaneously performing a transalkylation reaction and a dealkylation reaction of the heavy reformate stream in the reactor, where the composite zeolite catalyst is able to catalyze the transalkylation reaction and the dealkylation reaction simultaneously.2. The method of claim 1 , where the heavy reformate stream comprises at least 15 weight percent (wt. %) methylethylbenzene (MEB) and at least 50 wt. % trimethylbenzene (TMB) claim 1 , based on the total weight of the heavy reformate stream.3. The method of claim 1 , where the one or more impregnated metals are selected from Group VI and Group VII according to IUPAC nomenclature claim 1 , in which the metal in the zeolite catalyst is from 0.05 to 10 wt. % claim 1 , based on the total weight of the zeolite catalyst.4. The method of claim 1 , where the composite zeolite catalyst has a weight ratio of ZSM-5 to desilicated mesoporous mordenite of from greater than 0 to 1.0.5. The method of claim 1 , where the composite zeolite catalyst comprises a mixture of ZSM-5 and ...

Methods and apparatuses for producing xylene from propylbenzene

Methods and apparatuses are provided for producing xylene. A method includes combining a propylbenzene containing feed with a xylene raffinate stream, where the xylene raffinate stream is provided from a xylene recovery unit. The xylene raffinate stream and the propylbenzene containing feed are isomerized in an isomerization unit to produce an xylene isomerization effluent stream, where the xylene isomerization effluent stream includes aromatic compounds having 8, 9, or 10 carbons atoms. The aromatic compounds having 8 carbon atoms are separated from the aromatic compounds having 9 or 10 carbons, and the aromatic compounds having 8 carbons are fed to the xylene recovery unit. The aromatic compounds having 9 or 10 carbons are transalkylated with toluene to produce xylene.

METHODS AND APPARATUSES FOR PRODUCING XYLENE FROM LIGNIN

Methods and apparatuses are provided for producing a xylene product from a lignin supply. A method includes depolymerizing the lignin supply to produce a lignin aromatic stream, and isomerizing the lignin aromatic stream to produce an isomerized lignin stream. The desired xylene isomer is extracted from the isomerized lignin stream. 1. A method of producing a desired xylene isomer from lignin comprising:depolymerizing a lignin supply to produce a lignin aromatic stream;isomerizing the lignin aromatic stream to produce an isomerized lignin stream; andextracting the desired xylene isomer from the isomerized lignin stream.2. The method of further comprising:fractionating the lignin aromatic stream to produce a lignin center cut stream, a lignin light ends stream, and a lignin heavy ends stream; andwherein isomerizing the lignin aromatic stream comprises isomerizing the lignin center cut stream.3. The method of wherein extracting the desired xylene isomer comprises:producing a desired xylene isomer stream and a xylene raffinate stream, wherein the desired xylene isomer stream comprises the desired xylene isomer; andisomerizing the xylene raffinate stream in a xylene isomerization unit to produce the desired xylene isomer.4. The method of wherein depolymerizing the lignin supply comprises:contacting the lignin supply with a lignin catalyst at depolymerization conditions, wherein the lignin catalyst comprises a metal.5. The method of further comprising:dehydrogenating the isomerized lignin stream to produce a methyl enhanced aromatic stream; and whereinextracting the desired xylene isomer from the isomerized lignin stream comprises extracting the desired xylene isomer from the methyl enhanced aromatic stream.6. The method of wherein isomerizing the lignin aromatic stream and dehydrogenating the isomerized lignin stream produces a methyl enhanced aromatic compound from propyl benzene.7. The method of further comprising:producing xylene by transalkylating the methyl ...

METHODS AND SYSTEMS OF UPGRADING HEAVY AROMATICS STREAM TO PETROCHEMICAL FEEDSTOCK

Provided here are systems and methods that integrate a hydrodearylation process and a transalkylation process into an aromatic recovery complex. Various other embodiments may be disclosed and claimed. 1. A system for conversion of alkyl-bridged non-condensed alkyl multi-aromatic compounds to alkyl mono-aromatic compounds , the system comprising:{'sub': 9', '10, 'a first separator adapted to receive a feed stream containing one or more of heavy alkyl aromatic compounds and one or more alkyl-bridged non-condensed alkyl multi-aromatic compounds having at least two benzene rings connected by an alkyl bridge group with at least two carbons and the benzene rings being connected to different carbons of the alkyl bridge group, and produces a first product stream containing Cand Ccompounds and a second product stream containing one or more of heavy alkyl aromatic compounds and alkyl-bridged non-condensed alkyl multi-aromatic compounds;'}a hydrodearylation reactor fluidly coupled to the first separator and adapted to receive a hydrogen stream and the second product stream and to produce a third product stream in presence of a catalyst, the third product stream containing one or more alkyl mono-aromatic compounds; and{'sub': 8', '9+', '9', '10', '9+, 'a second separator fluidly coupled to the hydrodearylation reactor and adapted to receive the third product stream and to produce a benzene-containing stream, a toluene-containing stream, a C-rich stream, and a bottoms C stream, the system adapted to combine the first product stream containing Cand Ccompounds from the first separator and the bottoms C stream from the second separator.'}2. The system of claim 1 , further comprising:{'sub': '9+', 'a transalkylation/toluene disproportionation unit fluidly coupled to the second separator and adapted to receive the first product stream and one or more of the benzene-containing stream, the toluene-containing stream, and the bottoms C stream, and to produce alkyl mono-aromatic compounds ...

Catalyst composition comprising con-type zeolite and zsm-5-type zeolite, preparation and process using such composition

The invention relates to a catalyst composition comprising a) a carrier comprising: (i) of from 5 to 95 wt % of CON type zeolite, (ii) of from 5 to 95 wt % of ZSM-5 type zeolite; and (iii) of from 10 to 60 wt % of inorganic binder; and b) of from 0.001 to 10 wt % one or more metals selected from the group consisting of Group 6-11 of the IUPAC Periodic Table of Elements. The invention further relates to a process for preparing the catalyst composition and to a process for the conversion of an alkylaromatic hydrocarbons containing feedstock using a catalyst prepared by the present process.

PROCESS FOR PREPARING A MOLYBDENUM-PLATINUM-BASED CATALYST FOR THE SYNTHESIS OF BENZENE BY TRANSALKYLATION

A process for preparing a catalyst composition comprising (a) preparing a carrier comprising (i) mordenite in an amount in the range of from 20 to 80 wt %, based on total weight of carrier, (ii) ZSM-5 type zeolite in an amount in the range of from 10 to 70 wt %, based on total weight of carrier; and (iii) an inorganic binder in an amount in the range of from 10 to 50 wt %, based on total weight of carrier; (b) incorporating in the carrier molybdenum in an amount in the range of from 1 to 10 wt %, as metal based on total weight of catalyst composition, and subjecting the thus treated carrier to a temperature of from 100 to at most 300° C. and (c) incorporating in the molybdenum containing carrier obtained in step (b) platinum in an amount of from 0.005 to 1 wt %, as metal based on total weight of catalyst composition, and subjecting the thus treated carrier to a temperature of from 200 to at most 600° C.; and a process for conversion of alkylaromatic hydrocarbons containing feedstock using a catalyst prepared by said process. Process using the prepared catalyst composition for alkylaromatic hydrocarbon conversion. 1. A process for preparing a catalyst composition comprising:(a) preparing a carrier comprising (i) mordenite in an amount in the range of from 20 to 80 wt %, based on total weight of carrier, (ii) ZSM-5 type zeolite in an amount in the range of from 10 to 70 wt %, based on total weight of carrier; and (iii) an inorganic binder in an amount in the range of from 10 to 50 wt %, based on total weight of carrier;(b) incorporating in the carrier molybdenum in an amount in the range of from 1 to 10 wt %, as metal based on total weight of catalyst composition, and subjecting the thus treated carrier to a temperature of from 100 to at most 300° C.; and(c) incorporating in the molybdenum containing carrier obtained in step (b) platinum in an amount of from 0.005 to 1 wt %, as metal based on total weight of catalyst composition, and subjecting the thus treated ...

Guard Bed Material, Its Method of Making and Use

The present disclosure relates to a material preferably used in a guard bed, and having an increased capacity to adsorb catalyst poisons, as measured by collidine update at 200° C. The material is made by a method in which it is treated by being dried with a drying gas, preferably, at a temperature greater than about 200° C. The treated material may be used to remove impurities from untreated feed streams to, for example, aromatic alkylation and transalkylation processes, where such impurities act as catalyst poisons that cause deactivation of the acidic molecular sieve-based catalysts used, thereby increasing the cycle length of such catalysts. 1. A process for producing a mono-alkylated aromatic compound stream comprising the steps of:(a) providing a material comprising a molecular sieve, said material having a first collidine uptake at 200° C.;(b) drying said material with a drying gas at a temperature greater than about 200° C. to produce a guard bed material having a second collidine uptake at 200° C., wherein said second collidine uptake is greater than said first collidine uptake;(c) contacting an untreated stream having one or more impurities with said guard bed material of step (b) to remove at least a portion of said impurities and to produce a treated feed stream having a reduced amount of impurities, wherein said untreated stream comprising one or more alkylatable aromatic compound streams, optionally one or more alkylating agent streams; and(d) contacting said treated feed stream of step (c) and an alkylating agent stream with an alkylation catalyst composition under alkylation condition or a transalkylation catalyst composition under transalkylation conditions to produce an effluent stream comprising said mono-alkylated aromatic compound stream.2. The process of claim 1 , wherein said material is disposed in a guard bed vessel claim 1 , and wherein said contacting step (c) is conducted in-situ inside said guard bed vessel.3. The process of claim 1 , ...

Transalkylation of Heavy Aromatic Hydrocarbon Feedstocks

A process for producing xylene comprises contacting a first feed comprising C 9+ aromatic hydrocarbons, at least one C 6 -C 7 aromatic hydrocarbon and hydrogen with a first catalyst composition to dealkylate at least part of the C 9+ aromatic hydrocarbons containing C 2+ alkyl groups and to saturate the resulting C 2+ olefins to produce a second feed. The second feed is then contacted with a second catalyst composition under conditions effective to transalkylate at least part of the C 9+ aromatic hydrocarbons with at least part of the C 6 -C 7 aromatic hydrocarbon to produce a first product comprising xylene. Each of the first and second catalyst compositions is substantially free of amorphous alumina.

PROCESS FOR MAXIMIZING XYLENES PRODUCTION FROM HEAVY AROMATICS FOR USE THEREIN

A method for producing xylenes from a heavy reformate feed includes the steps of introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, introducing the dealkylation effluent to a splitter unit, separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, reacting the toluene stream and the C9 aromatics stream in the presence of the transalkylation catalyst to produce a transalkylation effluent, introducing the transalkylation effluent to the splitter unit, and separating the transalkylation effluent in the splitter unit. 1. A method for producing mixed xylenes from a heavy reformate feed , the method comprising the steps of: A method for producing mixed xylenes from a heavy reformate feed , the method comprising the steps of:introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst, wherein the heavy reformate comprises toluene and aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas;reacting the heavy reformate feed with the hydrogen gas in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, wherein the dealkylation reactor is at a dealkylation temperature, wherein the dealkylation reactor is at a dealkylation pressure, wherein the dealkylation reactor has a liquid hourly space velocity;introducing the dealkylation effluent to a splitter unit, where the dealkylation effluent comprises light gases, toluene, benzene, mixed ...

PROCESS AND DEVICE FOR THE INVERTED SEPARATION OF AROMATICS

The present invention relates to a process and to a device for the separation of a feedstock comprising benzene, toluene and C8+ compounds, in which: a toluene column (C10) is fed directly with a C7+ cut resulting from the bottom of a stabilization column (C11) positioned downstream of a transalkylation unit (P4); a C7− cut is withdrawn at the top of the toluene column (C10) and a C8+ cut is withdrawn at the bottom; a benzene column (C9) is fed with the C7− cut resulting from the toluene column (C10); an essentially aromatic cut resulting from an aromatics extraction unit (P1) is injected into the toluene column (C10) separately above the feeding of the C7+ cut or into the benzene column (C9). 1. Process for the separation of a feedstock comprising benzene , toluene and compounds having 8 or more carbon atoms , in a separation device comprising at least one reformate column (C1) , one aromatics extraction unit (P1) and one transalkylation unit (P4) , the effluents from the units being separated in the following distillation columns: benzene column (C9) , toluene column (C10) and stabilization column (C11) , the process comprising the following stages:the toluene column (C10) is fed directly with a C7+ cut resulting from the bottom of the stabilization column (C11) positioned downstream of the transalkylation unit (P4) in order to withdraw a top product from the toluene column (C10) enriched in benzene and in toluene and a bottom product from the toluene column (C10) enriched in compounds having 8 or more carbon atoms,the benzene column (C9) is fed with the top product from the toluene column (C10) in order to withdraw a benzene-enriched top product from the benzene column (C9) and a toluene-enriched bottom product from the benzene column (C9), andthe transalkylation unit (P4) is fed with the toluene-enriched bottom product from the benzene column (C9),in which the toluene column (C10) is fed with an essentially aromatic cut resulting from the aromatics extraction ...

Production of aromatic hydrocarbons from light alkanes

Provided is a method for producing aromatic hydrocarbons from light alkanes. A light alkane feed is contacted with catalyst particles in each of reactors, wherein each of the reactors is a fluidized bed reactor and arranged in parallel with each other in a furnace. At least a portion of the alkane feed is converted to aromatic hydrocarbons using the catalyst particles, wherein the aromatic hydrocarbons form a part of a reactor effluent stream. The reactor effluent streams from each of the reactors are merged to form a first merged effluent stream. The first merged effluent stream is separated into the aromatic hydrocarbons, light hydrocarbons, and a fuel gas.

TOLUENE METHYLATION WITH TRANSALKYLATION OF HEAVY AROMATICS

A method of producing a purified mixed xylene comprising: introducing toluene and methanol to an alkylation reactor; reacting the toluene and the methanol in the alkylation reactor to form a hydrocarbon stream comprising a first mixed xylene, wherein the alkylation reactor comprises an alkylation catalyst; separating the hydrocarbon stream into a toluene stream and a separated C stream; introducing the toluene stream to a transalkylation reactor with a transalkylation catalyst to produce a transalkylated stream comprising a second mixed xylene; adding the transalkylated stream to the hydrocarbon stream; and separating a Cproduct stream comprising the purified mixed xylene from the separated C stream. 1. A method of producing a purified mixed xylene comprising:introducing toluene and methanol to an alkylation reactor;reacting the toluene and the methanol in the alkylation reactor to form a hydrocarbon stream comprising a first mixed xylene, wherein the alkylation reactor comprises an alkylation catalyst;{'sub': '8+', 'separating the hydrocarbon stream into a toluene stream and a separated C stream;'}introducing the toluene stream to a transalkylation reactor with a transalkylation catalyst to produce a transalkylated stream comprising a second mixed xylene;adding the transalkylated stream to the hydrocarbon stream; and{'sub': 8', '8+, 'separating a Cproduct stream comprising the purified mixed xylene from the separated C stream.'}2. The method of claim 1 , wherein the alkylation catalyst comprises a phosphorus containing claim 1 , medium pore claim 1 , pentasil zeolite having a silica/alumina ratio of greater than or equal to 200.3. The method of claim 2 , wherein the phosphorus is present in an amount of 0.01 to 0.15 g per gram of zeolite.4. The method of claim 1 , wherein greater than or equal to 0.05 g of C aromatics per gram of toluene converted is produced in the alkylation reactor.5. The method of claim 1 , wherein the purified mixed xylene comprises greater ...

Process for the Production of Xylenes

In a process for producing para-xylene, a feed stream comprising C 6+ aromatic hydrocarbons is separated into a C 7− aromatic hydrocarbon-containing stream, a C 8 aromatic hydrocarbon-containing stream, and a C 9+ aromatic hydrocarbon-containing stream. The C 7− 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 C 8 aromatic hydrocarbon-containing stream, para-xylene is recovered from the ethylbenzene-depleted C 8 aromatic 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 9+ -containing stream with a transalkylation catalyst under conditions effective to convert C 9+ -aromatics to C 8− -aromatics and produce a transalkylated stream, which is recycled together with the isomerized stream to the para-xylene recovery section.

Process for the Production of Xylenes

In a process for producing para-xylene, a toluene-containing stream is contacted with a methylating agent under conditions effective to convert toluene to xylenes and produce a methylated effluent stream. Para-xylene is recovered from the methylated effluent stream to produce a para-xylene depleted stream and part of the para-xylene depleted stream is contacted with a xylene isomerization catalyst under liquid phase isomerization conditions effective to produce a first isomerized stream, while part of the para-xylene depleted stream is contacted with a xylene isomerization catalyst under vapor phase isomerization conditions effective to produce a second isomerized stream. The first and second isomerized streams are then recycled to the para-xylene recovery step. 1. A process for producing para-xylene , the process comprising:{'sub': 6+', '8, '(a1) separating a feed stream comprising C aromatic hydrocarbons into at least a toluene-containing stream and a Caromatic hydrocarbon-containing stream;'}(b1) contacting at least part of the toluene-containing stream with a methylating agent under conditions effective to convert toluene to xylenes and produce a methylated effluent stream;{'sub': '8', '(c1) recovering para-xylene from the Caromatic hydrocarbon-containing stream and the methylated effluent stream to produce at least one para-xylene depleted stream;'}(d1) contacting at least part of the at least one para-xylene depleted stream with a xylene isomerization catalyst under liquid phase conditions effective to isomerize xylenes in the para-xylene depleted stream and produce a first isomerized stream;(e1) contacting at least part of the at least one para-xylene depleted stream with a xylene isomerization catalyst under vapor phase conditions effective to isomerize xylenes and dealkylate or isomerize ethylbenzene in the para-xylene depleted stream and produce a second isomerized stream; and(f1) recycling at least part of the first and second isomerized streams to (c1).2 ...

Transalkylation of Heavy Aromatic Hydrocarbons

A process for producing xylene from C 9+ aromatic hydrocarbons comprises contacting a first feedstock comprising C 9+ aromatic hydrocarbons with a first catalyst in the presence of 0 wt. % or more of hydrogen under effective vapor phase dealkylation conditions to dealkylate part of the C 9+ aromatic hydrocarbons and produce a first product comprising benzene, toluene and residual C 9+ aromatic hydrocarbons. A second feedstock comprising C 9+ aromatic hydrocarbons and benzene and/or toluene is contacted with a second catalyst under effective liquid phase C 9+ transalkylation conditions to transalkylate at least part of the C 9+ aromatic hydrocarbons and produce a second product comprising xylenes.

Process for Converting Alkanes to Para-Xylene

Systems and methods are provided for forming para-xylene from aromatics-containing streams having reduced or minimized amounts of C2+ side chains. Reduced or minimized amounts of C2+ side chains can provide benefits for improving and/or allowing modification of transalkylation conditions, xylene isomerization conditions, or a combination thereof. Such aromatics-containing streams can be formed, for example, by conversion of methyl halide, methanol, syngas, and/or dimethyl ether to aromatics by an aromatic conversion process. The methyl halide, methanol, syngas, and/or dimethyl ether can be formed by conversion of methane.

PROCESS FOR MAKING MODIFIED SMALL-CRYSTAL MORDENITE, TRANSALKYLATION PROCESS USING SAME, AND MODIFIED SMALL-CRYSTAL MORDENITE

A modified UZM-14 zeolite is described. The modified UZM-14 zeolite has a Modification Factor of 6 or more. The modified UZM-14 zeolite may have one or more of: a Si/Al2 ratio of 14 to 30; a total pore volume in a range of 0.5 to 1.0 cc/g; at least 5% of a total pore volume being mesopores having a diameter of 10 nm of less; a cumulative pore volume of micropores and mesopores having a diameter of 100 Å or less of 0.25 cc/g or more; or a Collidine IR Bronsted acid site distribution greater than or equal to an area of 3/mg for a peak in a range of 1575 to 1700 cmafter desorption at 150° C. Processes of making the modified UZM-14 zeolite and transalkylation processes using the modified UZM-14 zeolite are also described. 1. A process for making a modified UZM-14 zeolite comprising:contacting a calcined UZM-14 zeolite with one or more of: nitric acid, or oxalic acid to form an acid washed UZM-14 zeolite;contacting the acid washed UZM-14 with one or more of: a sodium hydroxide solution, or a sodium bicarbonate solution to form a caustic washed UZM-14 zeolite; andion exchanging the caustic washed zeolite to form the modified UZM-14 zeolite.2. The process of wherein the calcined UZM-14 zeolite is formed by calcining a UZM-14 material to remove an organic template.3. The process of wherein the modified UZM-14 has a Modification Factor of 6 or more.4. The process of wherein the modified UZM-14 has a Si/Alratio of 14 to 30.5. The process of wherein the modified UZM-14 has a total pore volume in a range of 0.5 to 1.0 cc/g.6. The process of wherein the modified UZM-14 has at least 5% of a total pore volume being mesopores having a diameter of 10 nm of less.7. The process of wherein the modified UZM-14 has a cumulative pore volume of micropores and mesopores having a diameter of 100 Å or less of 0.25 cc/g or more.8. The process of wherein the modified UZM-14 has a Collidine IR Bronsted acid site distribution greater than or equal to an area of 3/mg for a peak in a range of 1575 ...

Disproportionation and Transalkylation of Heavy Aromatic Hydrocarbons

Disclosed herein is a process for producing para-xylene comprising the steps of: (a) contacting a feedstock comprising toluene with a first catalyst under effective vapor phase toluene disproportionation conditions to disproportionate said toluene and produce a first product comprising benzene, unreacted toluene and greater than equilibrium amounts of para-xylene; and (b) contacting a feedstock comprising C aromatic hydrocarbons and benzene with a second catalyst in the presence of 0 wt. % or more of hydrogen having a 0 to 10 hydrogen/hydrocarbon molar ratio under effective C transalkylation conditions to transalkylate said C aromatic hydrocarbons and produce a second product comprising xylenes. 1. A process for producing xylene from C aromatic hydrocarbons , the process comprising:(a) contacting a first feedstock comprising toluene with a first catalyst in the presence of 0 wt. % or more of hydrogen under effective vapor phase toluene disproportionation conditions to disproportionate at least part of said toluene and produce a first product comprising para-xylene; and{'sub': 9+', '9+', '9+, '(b) contacting a second feedstock comprising C aromatic hydrocarbons and toluene and/or benzene with a second catalyst in the presence of 0 wt. % or more of hydrogen under effective liquid phase C transalkylation conditions to transalkylate at least part said C aromatic hydrocarbons and produce a second product comprising xylenes.'}2. The process of claim 1 , wherein said first feedstock comprises fresh toluene or recycle toluene.3. The process of claim 1 , wherein said second feedstock comprises fresh C aromatic hydrocarbons or recycle C aromatic hydrocarbons.4. The process of claim 1 , wherein said second feedstock comprises fresh toluene or recycle toluene.5. The process of claim 1 , wherein said second feedstock comprises fresh benzene or recycle benzene.6. The process of claim 1 , further comprising:(c) separating any xylenes from the first product and/or the second ...