СПОСОБ КОНВЕРСИИ УГЛЕВОДОРОДОВ С ИСПОЛЬЗОВАНИЕМ СВЯЗАННОГО ЦЕОЛИТОМ ЦЕОЛИТНОГО КАТАЛИЗАТОРА

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

СПОСОБЫ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРОВ АРОМАТИЗАЦИИ

FIELD: chemistry. SUBSTANCE: invention discloses and describes methods for treating or regenerating spent catalysts containing a transition metal and a catalyst substrate, reforming methods, and a regenerated catalyst produced by the said methods. The method for treating the spent catalyst comprises: (1) contacting the spent catalyst with a halogen-containing stream containing chlorine and fluorine to produce a halogenated spent catalyst. The halogen-containing stream contains less than 100 ppm weight of the oxygen-containing compounds; (2) contacting the halogenated spent catalyst with a purge stream containing essentially inert gas; and (3) contacting the halogenated spent catalyst with a coke-removal gas stream containing oxygen; where the stream of coke oven gas contains less than 50 ppm weight of the halogenated compounds after step (2). Another method of treating the catalyst comprises: (i) bringing the spent catalyst into contact with a halogen-containing stream containing chlorine and fluorine to produce a halogenated spent catalyst; and (ii) bringing the halogenated spent catalyst into contact with a coke oven gas stream containing oxygen after step (i). In the halogenation step, fluorine and chlorine can be used together, or fluorine and chlorine can be used sequentially. The reforming method comprises: (a) bringing the hydrocarbon feed into contact with the aromatization catalyst under reforming conditions in the reactor system to produce an aromatic product; (b) carrying out step (a) for a period of time sufficient to form a spent aromatization catalyst; (c) bringing the spent aromatization catalyst into contact with a halogen-containing stream containing chlorine and fluorine to produce a halogenated spent catalyst; and (d) bringing the halogenated spent catalyst into contact with a coke oven gas stream containing oxygen. EFFECT: spent catalyst, which was initially halogenated, has a significantly lower start-up temperature than the spent catalyst, ...

СПОСОБ АЛКИЛИРОВАНИЯ С УЛУЧШЕННЫМ ОКТАНОВЫМ ЧИСЛОМ

Изобретение касается способа алкилирования углеводородов, в котором исходный материал, содержащий алкилируемое органическое соединение, реагирует с алкилирующим агентом с образованием алкилированного бензина, в присутствии катализатора. Алкилируемое органическое соединение представляет собой изоалкан, содержащий от 4 до 10 атомов углерода, и алкилирующий агент представляет собой олефин, содержащий от 2 до 10 атомов углерода. Катализатор содержит гидрогенизирующий функциональный компонент и компонент твердой кислоты, где исходный материал обрабатывают при условиях обработки, которые приводят к более высокому количеству образованной фракции C9+ продукта, чем условия обработки, оптимизированные для производства бензина, включая следующее условие a) и/или b): a) где исходный материал обрабатывают при среднечасовой массово-объемной скорости (WHSV) олефина, составляющей более 100% от среднечасовой массово-объемной скорости (WHSV), используемой для производства только бензина; b) где отношение ...

СПОСОБ ПОЛУЧЕНИЯ ЦЕОЛИТСОДЕРЖАЩЕГО КАТАЛИЗАТОРА

Изобретение относится к синтезу катализаторов, используемых, в частности, для превращения углеводородного сырья в компоненты высокоактивного моторного топлива, в ароматические углеводороды. Цеолитсодержащий катализатор получают смешением порошка цеолита ZSM-5 в аммонитной форме с солями цинка, аммония, промотирующими добавками, в качестве которых используют ортосиликат неодима (в виде суспензии), ацетаты рения и калия (в виде водных растворов). Способ включает фильтрацию смеси, промывку осадка, упаривание, формирование гранул со связующим - оксидом алюминия с добавкой оксида бора, высушивание, прокаливание при 500-550oС, последующую обработку при 450-550oС газовой смесью состава, мас.%: оксид углерода 4-5, диоксид углерода 4-12, водород 10-20, кислород 2-6, водяной пар 5-15, азот остальное, при скорости пропускания газовой смеси 1,0-200 ч-1. Формирование гранул со связующим осуществляют при соотношениях, мас.%: цеолит 58-62, оксид алюминия 35,5-37,5, оксид бора 2,5-4,5. Способ позволяет ...

СПОСОБЫ ПОЛУЧЕНИЯ КРИСТАЛЛИЧЕСКОГО ЦЕОЛИТА

Описан способ получения кристаллического цеолита из реакционной смеси, содержащей количество воды, достаточное только для того, чтобы, при желании, реакционной смеси можно было бы придать определенную форму. По данному способу реакционную смесь нагревают в условиях кристаллизации и в отсутствие внешней жидкой фазы, так что перед высушиванием кристаллов нет необходимости в удалении избыточной жидкости из закристаллизованного материала. Способ позволяет сократить количество воды для кристаллизации и получить формованные цеолиты без добавления связующего. 2 с. и 40 з.п.ф-лы.

ЦЕОЛИТ NU-86 И СПОСОБ ЕГО ПОЛУЧЕНИЯ

Цеолит, обозначенный как цеолит NU-86, имеющий молярный состав, выраженный формулой 100 XO2: ≅10 Y2O3: ≅20 R2/n0, где R - один или несколько катионов с валентностью n, X - кремний и/или германий, Y - один или несколько из алюминия, железа, галлия, бора, титана, ванадия, циркония, молибдена мышьяка, сурьмы, хрома и марганца, и имеющий картину дифракции рентгеновских лучей, включая линии, показанные в табл.1, причем цеолит получен из реакционной смеси, состоящей из XO2 (предпочтительно двуокись кремния), Y2O3 (предпочтительно окись алюминия) и катиона полиметилен - альфа, омега-диаммония. Этот цеолит пригоден в качестве катализатора для различных реакций. 2 с. и 6 з.п. ф-лы, 8 ил., 8 табл.

СПОСОБ КОНВЕРТИРОВАНИЯ АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ

Описывается способ конвертирования ароматических углеводородов C9+ в более легкие ароматические продукты, включающий стадию контактирования сырья, содержащего ароматические углеводороды C9+, бензол и/или толуол, с каталитической композицией, содержащей цеолит, имеющий показатель реакции связи от 0,5 до 3, гидрирующий компонент и, в случае необходимости, источник элемента группы IВ, для получения продукта, содержащего ксилолы, отличающийся тем, что для снижения активности гидрирования ароматических соединений каталитическую композицию, имеющую гидрирующий компонент, отрабатывают острым паром или источником серы. Технический результат - увеличение выхода более легких ароматических продуктов и упрощение процесса. 10 з.п.ф-лы, 3 ил., 6 табл.

СПОСОБ И УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ БЕНЗИНА ИЗ ЖИДКИХ УГЛЕВОДОРОДНЫХ ФРАКЦИЙ, ОКСИГЕНАТОВ И ОЛЕФИН-СОДЕРЖАЩИХ ГАЗОВ

Изобретение относится к способу получения бензинов, в котором в качестве сырья используют три потока, один из которых включает углеводородную фракцию, второй поток включает оксигенат, третий поток включает олефин-содержащую фракцию, содержащую олефины С2-С4в общем количестве от 10 до 50 мас.%,и где используют три реакционные зоны, заполненные цеолитным катализатором, с распределением углеводородной фракции в по меньшей мере одну реакционную зону, с распределением олефин-содержащей фракции в три реакционные зоны, с распределением оксигената в три реакционные зоны, причем разогрев слоя катализатора в каждой реакционной зоне составляет от 5 до 35°С, для каждой полки реактора температура катализата на выходе из слоя катализатора превышает температуру подачи сырья на данную полку реактора. Изобретение также касается установки для получения бензинов. Технический результат - сглаживание температурного профиля катализатора, получение бензина с ОЧИ выше 90 ед. при содержании ароматических углеводородов ...

СПОСОБ ПОЛУЧЕНИЯ ВЫСОКООКТАНОВЫХ БЕНЗИНОВЫХ ФРАКЦИЙ И АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ

Способ получения высокооктановых бензиновых фракций и ароматических углеводородов C-Cиз выкипающего в области температур кипения бензинолигроиновых фракций углеводородного сырья осуществляют путем его нагрева, испарения и перегрева до температуры переработки, последующего его контактирования при температуре 320-480°С и повышенном давлении с периодически регенерируемым катализатором, содержащим цеолит ZSM-5 или ZSM-11, охлаждения и частичной конденсации продуктов контактирования, их разделения путем сепарации и ректификации в стабилизационной колонне с выделением верхом этой колонны фракции(ций) углеводородных газов и кубом колонны стабильной бензиновой фракции, ректификации жидкой фракции в ректификационной колонне с выделением верхом этой колонны жидкого дистиллята и кубом колонны фракции тяжелого остатка, где сепарацию продуктов контактирования осуществляют при температуре 150-220°С или при температуре, обеспечивающей содержание мольной доли жидкости в продуктах контактирования, равное ...

Катализатор и способ его получения

Изобретение относится к катализатору и способу получения катализатора для производства бензинов или концентратов ароматических соединений. Катализатор особенно эффективен для процессов совместной переработки углеводородных фракций, оксигенатов и олефин-содержащих фракций. Достигается увеличение межрегенерационного периода работы катализатора до более 450 часов; увеличение выхода фракции С5+углеводородного продукта; снижение селективности образования метана и олефинов С2-С4. Катализатор включает цеолит ZSM-5 в количестве от 50.0 до 85.0 мас.%, связующее, оксиды цинка и редкоземельных элементов; объем пор катализатора от 0.15 до 0.26 см3/г, средний диаметр пор катализатора от 38 до 53 соотношение слабых и сильных кислотных центров катализатора от 2.2 до 3.5. Способ получения катализатора включает: смешение HZSM-5, пептизированного псевдобемита и затем кремнезоля с рН 8-10 для получения формовочной массы, формование, сушка и прокаливание формовочной массы с получением катализаторной композиции ...

СПОСОБ УВЕЛИЧЕНИЯ ВЫХОДА ЖИДКОГО УГЛЕВОДОРОДНОГО ПРОДУКТА

Изобретение относится к способу увеличения выхода жидкого углеводородного продукта до более 70 мас. % на поданную углеводородную фракцию в способе получения бензинов, в котором: в качестве сырья используют три потока, первый из которых включает углеводородную фракцию, второй поток включает оксигенат, третий поток включает олефинсодержащую фракцию, а) где олефинсодержащая фракция включает один или более олефинов, выбранных из группы, включающей: этилен, пропилен, нормальные бутилены, изобутилен, в общем количестве от 10 до 50 мас. %, и содержит от 0,5 до 8 мас. % водорода, б) посредством поддержания массовой скорости подачи сырья в диапазоне 1,5-1,9 ч-1, причем используют три реакционные зоны, заполненные цеолитным катализатором, первый поток подают по меньшей мере в одну реакционную зону, второй поток распределяют в три реакционные зоны, третий поток распределяют в три реакционные зоны, и поток продукта из первой реакционной зоны подается во вторую реакционную зону, и поток продукта из ...

СПОСОБ ПОЛУЧЕНИЯ ВЫСОКООКТАНОВЫХ БЕНЗИНОВЫХ ФРАКЦИЙ И АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ

Изобретение относится к получению высокооктановых бензиновых фракций и ароматических углеводородов С-Сиз углеводородного сырья, выкипающего в области температур кипения бензинолигроиновых фракций, и может быть использовано в нефтепереработке. Способ осуществляют путем нагрева выкипающего в области температур бензинолигроиновых фракций углеводородного сырья, испарения и перегрева до температуры переработки, последующего его контактирования при температуре 320-480°С и повышенном давлении с периодически регенерируемым катализатором, содержащим цеолит ZSM-5 или ZSM-11, охлаждения и частичной конденсации продуктов контактирования, их разделения путем сепарации и ректификации в стабилизационной колонне с выделением верхом этой колонны углеводородных газов и кубом колонны стабильной бензиновой фракции, ректификации жидкой фракции в ректификационной колонне с выделением верхом этой колонны жидкого дистиллята и кубом колонны фракции тяжелого остатка. Продукты реакции охлаждают и подвергают сепарации ...

СПОСОБЫ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРОВ АРОМАТИЗАЦИИ

... 1. Способ обработки отработанного катализатора, содержащего переходный металл и подложку катализатора, включающий:(1) приведение в контакт отработанного катализатора с галогенсодержащим потоком, содержащим хлор и фтор, с получением галогенированного отработанного катализатора;(2) приведение в контакт галогенированного отработанного катализатора с продувочным потоком, состоящим по существу из инертного газа; и(3) приведение в контакт галогенированного отработанного катализатора с потоком коксоудаляющего газа, содержащим кислород; где поток коксоудаляющего газа содержит менее чем 50 м.д. масс галогенсодержащих соединений.2. Способ по п. 1, отличающийся тем, что:стадию (1) осуществляют при температуре галогенирования в диапазоне от примерно 120°C до примерно 320°C; имолярное отношение Cl:F в галогенсодержащем потоке составляет от примерно 0,2:1 до примерно 10:1.3. Способ по п. 2, отличающийся тем, что указанный галогенсодержащий поток по существу не содержит кислородсодержащих соединений.4 ...

СПОСОБ ПОЛУЧЕНИЯ КОНЦЕНТРАТА АРОМАТИЧЕСКИХ УГЛЕВОДОРОДОВ ИЗ ЖИДКИХ УГЛЕВОДОРОДНЫХ ФРАКЦИЙ И УСТАНОВКА ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ

FIELD: chemistry. SUBSTANCE: invention relates to a method of producing a concentrate of aromatic hydrocarbons from liquid hydrocarbon fractions, which includes feeding starting components into a mixer, heating the mixed components, feeding the components into a reactor, wherein the heated components are converted in the presence of a zeolite-containing catalyst into aromatic hydrocarbons, dividing the obtained product into a liquid and a gas phase, at least partially feeding the obtained gas phase into the mixer, feeding the liquid phase into a fractionation column, from which the aromatic hydrocarbon concentrate is collected. The method is characterised by that it includes additionally feeding methanol into the mixer, heating the mixed components until full homogenisation thereof in the gas phase, feeding the hydrocarbon components remaining in the fractionation column after collection at least partially into the mixer of starting components, additionally dividing the liquid phase into liquid hydrocarbons and water, feeding the liquid hydrocarbons into the fractionation column, removing water, measuring the composition of the liquid aromatic hydrocarbons fed into the fractionation column, and, based on the results of measuring the composition of the liquid aromatic hydrocarbons, adjusting the ratio between the starting components fed into the mixer, and/or temperature of the fractionation column. The invention also relates to an apparatus. EFFECT: high efficiency of producing aromatic hydrocarbon concentrates and high content of alkylbenzenes, particularly xylenes. 10 cl, 4 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 558 955 C1 (51) МПК C07C 2/86 (2006.01) C07C 15/02 (2006.01) C10G 35/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2014133053/04, 12.08.2014 (24) Дата начала отсчета срока действия патента: 12.08.2014 (45) Опубликовано: 10.08.2015 Бюл. № 22 2 5 5 8 9 5 5 R U (54) СПОСОБ ...

UZM-45 АЛЮМОСИЛИКАТНЫЙ ЦЕОЛИТ, СПОСОБ ЕГО ПОЛУЧЕНИЯ И ПРОЦЕССЫ С ЕГО ИСПОЛЬЗОВАНИЕМ

1. Микропористый кристаллический цеолит, имеющий трехмерный каркас, по меньшей мере, из AlOи SiOтетраэдрических звеньев и эмпирический состав «как синтезирован» в безводном состоянии, выраженный эмпирической формулой:,где М представляет собой, по меньшей мере, один обмениваемый катион, выбранный из группы, состоящей из щелочных, щелочноземельных и редкоземельных металлов, "m" представляет собой мольное отношение М к (Al+Е) и составляет от 0 до 4,0, R представляет собой органоаммонийный катион, выбранный из группы, состоящей из холина, этилтриметиламмония (ЕТМА), диэтилдиметиламмония (DEDMA), тетраэтиламмония (TEA), тетрапропиламмония (ТРА), триметилпропиламмония, триметилбутиламмония, диметилдиэтаноламмония, гексаметония и их смесей, "r" представляет собой мольное отношение R к (Al+Е) и составляет от 0,25 до 4,0, "n" представляет собой средневзвешенную валентность М и составляет от 1 до 3, "p" представляет собой средневзвешенную валентность R и составляет от 1 до 2, Е представляет собой элемент, выбранный из группы, состоящей из галлия, железа, бора и их смесей, "x" представляет собой мольную долю Е и составляет от 0 до 1,0, "y" представляет собой мольное отношение Si к (Al+Е) и составляет от более 3 до 20 и "z" представляет собой мольное отношение О к (Al+Е) и имеет значение, определяемое уравнением:z=(m·n+r·p+3+4·y)/2и характеризующийся рентгенограммой, по меньшей мере, с межплоскостными расстояниями d и интенсивностями, приведенными ниже:и термической стабильностью до температуры по меньшей мере 400°С.2. Цеолит по п.1, в котором М выбран из группы, состоящей из лития, натрия, калия, рубидия, цезия, кальция, стронция, бария и их смесей.3. Цеолит по п.1, в котором R пре� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2012 151 832 A (51) МПК C01B 39/48 (2006.01) C01B 39/02 (2006.01) B01J 29/70 (2006.01) C07C 2/12 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: ...

АЛЮМОСИЛИКАТНЫЙ ЦЕОЛИТ UZM-7, СПОСОБ ЕГО ПОЛУЧЕНИЯ И СПОСОБ ЕГО ИСПОЛЬЗОВАНИЯ

... 1. Микропористый кристаллический цеолит, имеющий трехмерную структуру с по меньшей мере тетраэдрическими единицами AlOи SiOи эмпирическим составом синтезированного безводного продукта, выраженным эмпирической формулой:,где М представляет собой по меньшей мере один обменный катион, выбранный из группы, состоящей из щелочных, щелочноземельных и редкоземельных металлов, "m" представляет собой мольное отношение М к (Al+Е) и варьируется от 0 до приблизительно 2,0, R представляет собой катион органиламмония, выбранный из группы, состоящей из холина, этилтриметиламмония (ЭТМА), диэтилдиметиламмония (ДЭДМА), тетраэтиламмония (ТЭА), тетрапропиламмония (ТПА), триметилпропиламмония, триметилбутиламмония, диметилдиэтаноламмония, гексаметония и их смесей, "r" представляет собой мольное отношение R к (Al+Е) и имеет значение от приблизительно 0,25 до приблизительно 4,0, "n" представляет собой средневзвешенную валентность М и имеет значение от приблизительно 1 до приблизительно 3, "p" представляет собой ...

ZINKHALTIGER ZEOLITH-L.

Verwendung eines Katalysators, der einen Zeolith, ein Edelmetall der Platingruppe und ein zusätzliches Metall enthält in der Aromatisierung von Kohlenwasserstoffen mit 5 bis 12 Kohlenstoffatomen.

VERFAHREN ZUR REGENERIERUNG EINES DURCH SCHWEFELVERUNREINIGTEN UMWANDLUNGSKATALYSATORS.

VERFAHREN ZUR OKTANZAHLSTEIGERUNG UND ZUR VERRINGERUNG DES SCHWEFELGEHALTES VON OLEFINISCHEN BENZINEN.

Verfahren zur katalytischen Umwandlung von Kohlenwasserstoffen

NAPHTA-AROMATIZATIONSVERFAHREN

Barium-exchanged zeolite L catalyst contg. platinum

Compsns. useful as catalysts comprise: (a) a zeolite of type L; (b) a metal of Group VIII, pref. Pt; and (c) Ca, Sr or esp. Ba, pref. introduced into the zeolite by ion-exchange. Pref. the majority of the zeolite crystals are larger than 50 nm. A pref. compsn. (I) comprises zeolite L with 1-20 wt.% Ba and 0.1-1.5 wt.% Pt. Pref. at least 80% of the zeolite particles are larger than 100 nm. (I) can be used for reforming, e.g. of straight-run naphtha, in presence of H2: pref. conditions are 430-550 deg , a pressure of 3.5-21 atmospheres, a ratio of H2/hydrocarbon of 2:1 to 6:1, and LHSV 0.1-10. The catalyst is deactivated by S. which must be removed from the feestock, e.g. by hydrofining. The compsns. are useful for reforming, dehydrocyclisation (esp. of C6-C8 paraffins) to aromatics, dealkylation of toluene to benzene, and dehydroisomerisation of alkylcyclopentanes to aromatics. Prod. yields are high: e.g. selectivity of conversion of n-hexane to benzene can be 90%. Catalyst life is adequate ...

VERFAHREN ZUR HERSTELLUNG EINES KRISTALLINEN ALUMINIUMSILIKAT-L-ZEOLITHKATALYSATORS UND VERWENDUNG DES AUF DIESE WEISE ERHALTENEN KATALYSATORS

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.

PROCESS FOR INCREASING THE OCTANE NUMBER OF A LIGHT GASOLINE FRACTION

... 1386004 Cracking hydrocarbons SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ NV 9 Feb 1972 [11 Feb 1971 4 March 1971] 6061/72 Heading C5E A naphtha consisting mainly (85% or more) of C 5 and C 6 paraffins, low in aromatics (5% or less) and having a ratio (Y) of iso/normal C 6 hydrocarbons of 2 or more is hydrocracked selectively to remove normal paraffins and improve the octane rating. The feed must contain a proportion (X%) of C 6 paraffins of 25% or more, and 65Y must be equal to or more than 2x+80. The feed may be the product of an isomerization step, and may contain sulphur. Iso-pentanes may be removed from it before cracking, and blended with the product after removal of C 4 and lighter. The catalyst may include a porous zeolite, and may be sulphided. Six process schemes are described: in scheme I a feed is distilled to take off iso-pentanes, the topped naphtha is then isomerized and hydrocracked and again distilled to take off butanes and lighter, the distillate from the first distillation ...

ZEOLITE L

PROCESS FOR UPGRADING A SULPHUR-CONTAINING FEEDSTOCK

Selective Conversion Process

... 1,178,427. Cracking catalysts. ESSO RESEARCH & ENG. CO. 26 May, 1967 [7 June, 1966], No. 24595/67. Heading B1E. [Also in Divisions Cl and C5] A catalyst for selectively hydrocracking straight-chain hydrocarbons contained in a hydrocarbon feedstock comprises a rare earth metal-containing crystalline aluminosilicate zeolite having uniform pore openings of less than 6 Angstrom units. The zeolite may be zeolite A or natural or synthetic erionite. It may be base-exchanged with a rare earth metal. Rare earth metals are defined as those having atomic numbers from 57 to 71 inclusive, scandium and yttrium. The catalysts may also contain cadmium or zinc. A hydrogenation metal component such as cobalt, nickel, platium, palladium, ruthenium, rhodium, osmium or iridium in the form of the free metal, oxide, sulphide or mixtures thereof may also be included.

Catalytically upgrading sulphur rich naphtha

Hydrocarbon conversion process

Molecular sieves of uniform pore of size sufficiently large to absorb benzene and containing metals, or oxides thereof, in the inner absorption regions are used as catalysts and of the appropriate conditions and at elevated temperatures for the following reactions of hydrocarbons (1) hydrocracking, polymerization, alkylation, hydroforming, isomerization, or dehydrogenation, the metal being platinum, iron, cobalt or nickel, (2) hydrogenation, the metals being platinum, iron, cobalt or nickel, (3) hydrocracking, polymerization, hydroforming, hydrogenation or dehydrogenation, the metals being chromium, tungsten, molybdenum, vanadium, or rhenium, (4) hydrocracking, polymerization, hydrogenation or dehydrogenation, the metal being copper and (5) polymerization, the metal being aluminium. Examples relate to (a) dehydrogenation of a tetralin to a naphthalene, cyclohexane to benzene, methylcyclohexane to toluene, and butanes to butenes; (b) hydrogenation of propylene to propane; (c) alkylation ...

METHOD OF REFORMING HYDROCARBONS

Zeolite catalyst

A zeolite catalyst useful for dehydrocyclizing acyclic hydrocarbons contains a type L zeolite, a Group VIII metal, preferably platinum, and an alkaline earth metal, preferably barium. The catalyst preferably contains from 0.1% to 1.5% by weight platinum and from 1% to 20% by weight barium.

PROCESS FOR THE PRODUCTION OF AROMATIC COMPOUNDS

... 1381427 Aromatization MOBIL OIL CORP 12 April 1973 [17 May 1972] 17587/73 Heading C5E Aromatic hydrocarbons are produced by contacting a feed comprising paraffins, olefins and/or naphthenes and no more than 15 wt. per cent aromatics (at least 50 wt. per cent of the feed boiling no higher than 250‹ F.) with a zeolite of the ZSM.5, ZSM.8 or ZSM.11 types, at a pressure of 1-35 atmos. absolute, a WHSV of 0À6-15, and a temperature of at least 650‹ F. when the feed contains at least 35 wt. per cent olefins and at least 850‹ F. when the feed contains less than 35 wt. per cent olefins. The reaction is preferably carried out in the absence of added H 2 . The zeolites are preferably baseexchanged with H+, NH 4 + or Zn++, and may be composited with a porous matrix such as Al 2 O 3 , SiO 2 , SiO 2 -Al 2 O 3 or clay.

Molecular sieve catalyst suitable for hydrocarbon conversion processes

A hydrocarbon conversion catalyst of uniform pore size 6-15 is prepared by heating a mixture of solutions of sodium silicate and aluminate to obtain precipitated sodium aluminosilicate, base-exchanging with an ammonium compound and calcining the product to obtain the hydrogen form of the crystal which is then impregnated with a metal compound of the platinum group or with an oxide of Mo, Cr, W, V, Ni, Cu or Co or a mixture thereof; the proportions of the starting materials are such that the silica/alumina ratio in the final molecular sieve support is in the range 2,2-10:1 and the Na content is not more than 10% (calculated as Na2O). Specification 824,543 is referred to.

Low-sulfur reforming processes.

VERFAHREN ZUR ERHOEHUNG DER OKTANZAHL EINER LEICHTEN BENZINFRAKTION

PROCEDURE FOR THE INCREASE OF THE OCTANE NUMBER OF A LIGHT GASOLINE PARLIAMENTARY GROUP

PROCEDURE FOR THE REFORMATION OF OIL HYDROCARBONS

NEW ZEOLITE SSZ-31

POROUS INORGANIC MACRO STRUCTURES AND PROCEDURES FOR THE PRODUCTION THE SAME

ZEOLITES

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

PREPARING OF L-ZEOLITE.

PROCEDURE FOR THE RECOVERY OF A DEACTIVATED CATALYST.

VERY LOW-TEMPERATURE RECOVERY OF REFORMATION CATALYSTS DEACTIVATED BY COKE

PROCEDURE FOR THE IMPROVEMENT A SULFUR OF A CONTAINING REPLACEMENT MATERIAL.

ZINKHALTIGER ZEOLITE L.

PRODUCTION OF ZEOLITE L.

PROCEDURE FOR THE DISTANCE OF HALOGENIERTEN CONNECTIONS FROM A GAS OR A LIQUID OF MEANS OF A AT LEAST A METALLIC ELEMENT CONTAINING COMPILATION

Procedure for cracking hydrocarbons

High-silica zeolite ssz-37 and methods of making and using same

Zeolite ssz-45

ZEOLITE L OF CHARACTERISTIC MORPHOLOGY

CATALYTIC ISOMERIZATION OF SULFUR-CONTAINING FEEDSTOCKS

CONVERTING S AND N CONTAINING ORGANIC CHARGE WITH ZSM-20 CATALYST

ZEOLITES

Catalyst compositions comprising molecular sieves, their preparation and use in conversion processes

MOLECULAR SIEVE SSZ-64

METHOD FOR PRODUCING AROMATIC HYDROCARBONS

Multi-stage reforming process to produce high octane gasoline

ZEOLITES

UPGRADING GASOLINE DERIVED FROM SYNTHESIS GAS

CALYTIC REFORMING

ZEOLITE CATALYST AND PRODUCTION OF AROMATIC HYDROCARBONS

Gasoline upgrading process

Monofunctional reforming catalyst containing bismuth

NAPHTHA CRACKING

CONVERSION PROCESS USING LEACHED MORDENITE CATALYST

Naphtha reforming catalyst and process

Method of removing reactive metal from a metal-coated reactor system

REFORMING PROCESS HAVING A HIGH SELECTIVITY AND ACTIVITY FOR DEHYDROCYCLIZATION, ISOMERIZATION, AND DEHYDROISOMERIZATION

HYDROCARBON CONVERSION PROCESS

METHOD OF DEHYDROCYCLIZING ALKANES

PROCESS FOR UP-GRADING STEAM-CRACKING PRODUCTS

PROCESS FOR PRODUCTION OF AROMATIC HYDROCARBONS

A process for producing aromatic hydrocarbons in a high yield by introducing a naphtha fraction the cyclopentane content of which is controlled to not more than 1% by weight, or the methylpentane content is controlled to not more than 10% by weight, in a catalytic reaction tower, and contacting with a catalyst comprising a large pore zeolite containing at least one of Group VIII metals of the Periodic Table. In this process, the catalyst cycle is greatly lengthened.

METHOD FOR SUPPRESSING HYDROGENOLYSIS OF NOBLE METAL/LOW ACIDITY ZEOLITES

F-4589 METHOD FOR SUPPRESSING HYDROGENOLYSIS OF MOBLE METAL/LOW ACIDITY ZEOLITES USED IN AROMATIZING PARAFFINS A process for converting a C6-C12 paraffinic hydrocarbon feed to aromatics by contacting the feed with a noble metal/low acidity medium pore size zeolite catalyst in a conversion zone by modifying the noble metal component of the catalyst to its sulfide form by either presulfiding the catalyst or adding at least one of H2S, SO2 or an organic sulfur compound to the feed in an amount effective to suppress hydrogenolysis and increase aromatic selectivity of the catalyst.

UPGRADING GASOLINE DERIVED FROM SYNTHESIS GAS

Case 5059 UPGRADING GASOLINE DERIVED FROM SYNTHESIS GAS The present invention relates to a process for upgrading low grate gasoline made from synthesis gas, especidally the gasoline made from coal-based processes. The process comprises contacting in the vapour phase the low-grade gasoline either alone or admixed with a C3/C4 hydrocarbon feed with a gallium/aluminosilicate catalyst. The product gasoline so formed has an octane rating RON (clear) above 100 and a bromine number below 2. The process enables synthesis gas ant coal to be used as a source of high grade gasoline.

PRODUCTION OF AROMATIC HYDROCARBONS FROM OLEFINS

This invention relates to a process for producing aromatic hydrocarbons suitable for use as gasoline blending components. In the process a mixed hydrocarbon feedstock comprising a C5-C12 hydrocarbon fraction containing olefins and an (un)saturated C3-C4 hydrocarbon is brought into contact in the vapour phase with an aluminosilicate having a gallium compound deposited thereon or having gallium ions exchanged with cations thereir. The resultant product shows considerable improvement in RON and MON and is therefore ideal for blending with gasoline. Hydrogen is formed as a valuable by-product.

NAPHTHA HYDROFORMING PROCESS

PROCESS FOR THE PRODUCTION OF AROMATIC COMPOUNDS

CATALYTIC ISOMERIZATION OF SULFUR-CONTAINING FEEDSTOCKS

CATALYTIC ISOMERIZATION OF SULFUR-CONTAINING FEEDSTOCKS Catalytic isomerization of paraffinic feedstocks containing at least about 2 ppm by weight sulfur is effected using an isomerization catalyst comprising a hydrogenation/dehydrogenation catalyst supported on molecular sieve without undue loss of catalytic activity or selectivity by maintaining the water content of the feedstock below about 5 ppm by weight water.

ISOMERIZATION PROCESS

PROCESS FOR INCREASING THE OCTANE NUMBER OF A LIGHT GASOLINE FRACTION

DEHYDROCYCLIZATION PROCESS WITH DOWNSTREAM DIMETHYLBUTANE REMOVAL

In the present invention, dimethylbutanes are removed from the raffinate component of the feed to a dehydrocyclization process. Thus, according to a preferred embodiment, a process is provided for producing aromatics by the following steps: (a) contacting fresh paraffins rich feed hydrocarbons, containing 0.1 to 20.0 wt.% dimethylbutanes with a highly selective dehydrocyclization catalyst in a reaction zone, under dehydrocyclization reaction conditions, to convert paraffins to aromatics and obtain an aromatics rich effluent; (b) separating aromatics from the effluent to obtain an aromatics lean raffinate; (c) removing dimethylbutanes from the raffinate to obtain a raffinate of reduced dimethylbutane content; and (d) recycling the raffinate of reduced dimethylbutane content to the reaction zone. Preferably, the dehydrocyclization catalyst used is a nonacidic, monofunctional catalyst. Platinum on L zeolite is a particularly preferred highly selective dehydrocyclization catalyst for use in ...

AROMATIC HYDROCARBON PRODUCING CATALYST, AND ITS PREPARATION

METHOD OF PROCESSING PETROLEUM DISTILLATES

The invention relates to petroleum chemistry, in particular to method for producing high-octane gasoline fractions from straight petrol distillates. The inventive method for processing petrol distillates into gasoline fractions having an end boiling point equal to or less than 195 ~C and an octane number equal to or greater than 80 according to a motor method, consists in transforming a hydrocarbon material in a presence of a porous catalyst at a temperature ranging from 200 ~C to 250 ~C, a pressure equal to or less than 2 MPa and mass rates of a hydrocarbon mixture equal to or less than 10 h-1. Ceolite having an alumosilicate composition modified by metals having silicate or alumophosphate compositions is used as a catalyst. The inventive method makes it possible to simplify the process and increase the production of high- octane gasoline fractions using the straight petrol distillates having an extended hydrocarbon composition as a feed stock, said distillates not being pre-fractionated ...

PROCESS FOR UPGRADING A GASOLINE

PROCESS FOR THE PRODUCTION OF AROMATIC COMPOUNDS

METHOD OF REGENERATING AROMATIZATION CATALYSTS

Methods for treating or rejuvenating a spent catalyst are disclosed. Such methods can employ a step of halogenating the spent catalyst, followed by decoking the halogenated spent catalyst. The halogenation step can utilize fluorine and chlorine together, or fluorine and chlorine can be applied sequentially.

MULTIMETALLIC AND MULTIGRADIENT REFORMING CATALYST FOR CONVERTING PARAFFINS TO AROMATICS

A reforming process, selective for the dehydrocyclization of paraffins to aromatics, is improved by using a bound catalyst containing multiple Group VIII (8-10) noble metals having different gradients within the catalyst and a nonacidic large-pore molecular sieve. The use of this catalyst results in greater selectivity of conversion of paraffins to aromatics and improved catalyst stability, particularly in the presence of small amounts of sulfur.

PROCESS FOR UPGRADING A SULPHUR-CONTAINING FEEDSTOCK

T 5408 PROCESS FOR UPGRADING A SULPHUR-CONTAINING FEEDSTOCK Process for upgrading a sulphur-containing feedstock comprising a hydrocarbon mixture substantially boiling in the gasoline range which process comprises contacting the feedstock with a catalyst which comprises a crystalline (metallo)silicate having an X-ray diffraction pattern containing the four strongest lines at interplanar spacings (d) expressed in A, of 11.1 + 0.2, 10.0 + 0.2, 3.84 + 0.07 and 3.72 + 0.06, and recovering therefrom a product boiling in the gasoline range of increased aromaticity and decreased sulphur content.

ZEOLITE NU-85

A zeolite, designated NU-85, is an intergrowth of zeolites EU-1 and NU-87. The zeolite is a useful catalyst in a wide variety of hydrocarbon conversion reactions including isomerisation and alkylation.

METHOD FOR PRETREATING A REFORMONG CATALYST

Supported Group VIII noble metal reforming catalysts are pretreated with an unsaturated aliphatic hydrocarbon at elevated temperatures, thereby lower activity during initial reforming operation and reducing gas production during the initial operation.

Method for producing monocyclic aromatic hydrocarbons

A method for producing monocyclic aromatic hydrocarbons of 6 to 8 carbon number from a feedstock oil having a 10 volume % distillation temperature of at least 140° C. and a 90 volume % distillation temperature of not more than 380° C., the method including: a cracking and reforming reaction step of obtaining a product containing monocyclic aromatic hydrocarbons of 6 to 8 carbon number from the feedstock oil, a refining and collection step of refining and collecting monocyclic aromatic hydrocarbons of 6 to 8 carbon number that have been separated from the product, a hydrogenation reaction step of hydrogenating a heavy fraction of 9 or more carbon number separated from the product, and a recycling step of returning the heavy fraction hydrogenation reaction product obtained in the hydrogenation reaction step to the cracking and reforming reaction step.

Reforming process with integrated fluid catalytic cracker gasoline and hydroprocessed cycle oil

A reforming process includes integrating catalytic cracking product naphtha dehydrogenation and naphtha from a hydrocracking zone and feeding them to a dehydrogenation zone. The dehydrogenation zone includes a first portion of reforming catalyst from a catalyst regenerator that moves downward through the dehydrogenation zone. A product stream from the dehydrogenation zone flows to an aromatics unit and is separated into an aromatic-rich extract and a raffinate. Straight run naphtha and the raffinate are introduced to a first reforming zone that includes a second portion of reforming catalyst. The reforming catalyst moves through the first reforming zone then is removed from the bottom of each of the first reforming zone and the dehydrogenation zone and is fed to a second reforming zone. An effluent from the first reforming zone is fed to a plurality of reforming zones. The reforming catalyst moves downward through the multiple refoiniing zones then to a regenerator.

METHODS FOR PRODUCING MESOPOROUS ZEOLITE MULTIFUNCTIONAL CATALYSTS FOR UPGRADING PYROLYSIS OIL

A method of making a multifunctional catalyst for upgrading pyrolysis oil includes contacting a hierarchical mesoporous zeolite support with a solution including at least a first metal catalyst precursor and a second metal catalyst precursor, each or both of which may include a heteropolyacid. The hierarchical mesoporous zeolite support may have an average pore size of from 2 nm to 40 nm. Contacting the hierarchical mesoporous zeolite support with the solution deposits or adsorbs the first metal catalyst precursor and the second catalyst precursor onto outer surfaces and pore surfaces of the hierarchical mesoporous zeolite support to produce a multifunctional catalyst precursor. The method further includes removing excess solution and calcining the multifunctional catalyst precursor to produce the multifunctional catalyst comprising at least a first metal catalyst and a second metal catalyst deposited on the outer surfaces and pore surfaces of the hierarchical mesoporous zeolite support. 1. A method of making a multifunctional catalyst for upgrading pyrolysis oil , the method comprising: the hierarchical mesoporous zeolite support has an average pore size of from 2 nanometers to 40 nanometers as determined by Barrett-Joyner-Halenda (BJH) analysis;', 'the first metal catalyst precursor, the second metal catalyst precursor, or both, comprises a heteropolyacid having at least one heteroatom selected from the group consisting of phosphorous, silicon, germanium, arsenic, and combinations of these; and', 'the contacting deposits the first metal catalyst precursor and the second metal catalyst precursor onto outer surfaces and pore surfaces of the hierarchical mesoporous zeolite support to produce a multifunctional catalyst precursor;, 'contacting a hierarchical mesoporous zeolite support with a solution comprising at least a first metal catalyst precursor and a second metal catalyst precursor, whereremoving excess solution from the multifunctional catalyst precursor; ...

METHODS FOR PRODUCING MESOPOROUS ZEOLITE MULTIFUNCTIONAL CATALYSTS FOR UPGRADING PYROLYSIS OIL

A method of making a multifunctional catalyst for upgrading pyrolysis oil includes contacting a hierarchical mesoporous zeolite support with a solution including at least a first metal catalyst precursor and a second metal catalyst precursor, each or both of which may include a heteropolyacid. The hierarchical mesoporous zeolite support may have an average pore size of from 2 nm to 40 nm. Contacting the hierarchical mesoporous zeolite support with the solution deposits or adsorbs the first metal catalyst precursor and the second catalyst precursor onto outer surfaces and pore surfaces of the hierarchical mesoporous zeolite support to produce a multifunctional catalyst precursor. The method further includes removing excess solution and calcining the multifunctional catalyst precursor to produce the multifunctional catalyst comprising at least a first metal catalyst and a second metal catalyst deposited on the outer surfaces and pore surfaces of the hierarchical mesoporous zeolite support. 112-. (canceled)13. A multifunctional catalyst for upgrading pyrolysis oil produced by a method comprising: the hierarchical mesoporous zeolite support has an average pore size of from 2 nanometers to 40 nanometers as determined by Barrett-Joyner-Halenda (BJH) analysis;', 'the first metal catalyst precursor, the second metal catalyst precursor, or both, comprises a heteropolyacid; and', 'the contacting deposits the first metal catalyst precursor and the second metal catalyst precursor onto outer surfaces and pore surfaces of the hierarchical mesoporous zeolite support to produce a multifunctional catalyst precursor;, 'contacting a hierarchical mesoporous zeolite support with a solution comprising at least a first metal catalyst precursor and a second metal catalyst precursor, whereremoving excess solution from the multifunctional catalyst precursor; andcalcining the multifunctional catalyst precursor to produce the multifunctional catalyst comprising at least a first metal catalyst ...

PROCESS TO PREPARE PROPYLENE

The invention is directed to a process to prepare propylene from a hydrocarbon feedstock comprising olefin hydrocarbon compounds by contacting the feedstock with a mixture of a heterogeneous cracking catalyst and a heterogeneous dehydrogenation catalyst as present in one or more packed beds thereby obtaining propylene and other reaction products. 1. A process to prepare propylene(i) from a hydrocarbon feedstock comprising olefin hydrocarbon compounds by contacting the feedstock with a mixture of a heterogeneous cracking catalyst and a heterogeneous dehydrogenation catalyst as present in one or more packed beds thereby obtaining propylene and other reaction products, wherein the cracking catalyst and the dehydrogenation catalyst are present in one or more packed beds in an in-series configuration and wherein the hydrocarbon feedstock, formed propylene and other reaction products will flow from an up-flow region to a down-flow region following a flow path and wherein in the direction of the flow path the concentration of the dehydrogenation catalyst in the bed increases compared to the cracking catalyst and/or(ii) from a hydrocarbon feedstock comprising paraffinic hydrocarbon compounds by contacting the feedstock with a mixture of a heterogeneous cracking catalyst and a heterogeneous dehydrogenation catalyst as present in one or more packed beds thereby obtaining propylene and other reaction products, wherein the cracking catalyst and the dehydrogenation catalyst are present in one or more packed beds in an in-series configuration and wherein the hydrocarbon feedstock, formed propylene and other reaction products will flow from an up-flow region to a down-flow region following a flow path and wherein in the direction of the flow path the concentration of the dehydrogenation catalyst in the bed decreases compared to the cracking catalyst.2. The process according to claim 1 , wherein the content of olefins having 4 or more carbon atoms in the feedstock of process (i) is ...

PROCESSING OF PARAFFINIC NAPHTHA WITH MODIFIED USY ZEOLITE DEHYDROGENATION CATALYST

Methods for processing paraffinic naphtha include contacting a paraffinic naphtha feedstock with a catalyst system in a dehydrogenation reactor. The catalyst system includes a framework-substituted ultra-stable Y (USY)-type zeolite to produce a dehydrogenated product stream. The catalyst system includes a framework-substituted ultra-stable Y (USY)-type zeolite. The framework-substituted USY-type zeolite has a modified USY framework. The modified USY framework includes a USY aluminosilicate framework modified by substituting a portion of framework aluminum atoms of the USY aluminosilicate framework with substitution atoms independently selected from the group consisting of titanium atoms, zirconium atoms, hafnium atoms, and combinations thereof. A dehydrogenation catalyst for dehydrogenating a paraffinic naphtha includes the framework-substituted ultra-stable Y (USY)-type zeolite. 2. The method of claim 1 , wherein the framework-substituted USY-type zeolite contains from 0.01% to 5% by mass substitution atoms claim 1 , as calculated on an oxide basis claim 1 , based on the total mass of the framework-substituted USY-type zeolite.3. The method of claim 1 , wherein:the framework-substituted USY-type zeolite contains from 0.01% to 5% by mass substitution atoms, as calculated on an oxide basis, based on the total mass of the framework-substituted USY-type zeolite; andthe substitution atoms comprise a combination selected from the group consisting of (a) titanium atoms and zirconium atoms, (b) titanium atoms and hafnium atoms, (c) zirconium atoms and hafnium atoms, and (d) titanium atoms, zirconium atoms, and hafnium atoms.4. The method of claim 1 , wherein:the framework-substituted USY-type zeolite contains from 0.01% to 5% by mass substitution atoms, as calculated on an oxide basis, based on the total mass of the framework-substituted USY-type zeolite; andthe substitution atoms comprise titanium atoms and zirconium atoms.5. The method of claim 1 , wherein the ...

SINGLE-LOOP OCTANE ENRICHMENT

The present invention provides apparatuses and processes for producing high octane fuel from synthesis gas. The process combines transalkylation and zeolite-forming/aromatization in conjunction with a single recycle loop configuration in order to effectively promote the fuel quality, particularly octane rating. The process involves adding a step for enriching octane of the fuel coming from the single recycle loop process. Preferably, the enrichment step takes place in an octane enrichment reactor containing two different catalysts, a zeolite-forming/aromatization catalyst followed by a transalkylation catalyst. The final fuel product preferably has an octane of about 92 to about 112. 111-. (canceled)12. A system for making high octane fuel product comprisinga) a single loop system for making a medium octane fuel; andb) an octane enrichment reactor comprising a zeolite forming catalyst and a transalkylation catalyst.13. The system of claim 12 , wherein the single loop system for making a medium octane fuel comprisesi. a first reactor containing a first catalyst for converting synthesis gas to methanol and water;ii. a second reactor containing a second catalyst for converting methanol to dimethylether;iii. a third reactor containing a third catalyst for converting methanol and dimethylether to fuel and heavy gasoline;iv. a fourth reactor containing a fourth catalyst for converting the heavy gasoline to isoparaffins, naphthenes, and less substituted aromatics; andv. a separator for separating a product exiting the third reactor into a first stream containing the medium octane fuel, a second stream containing water, and a third stream containing unreacted synthesis gas.14. The system of claim 12 , wherein the single loop system for making a medium octane fuel comprisesi. a first reactor containing a first catalyst for converting synthesis gas to methanol and water;ii. a second reactor containing a second catalyst for converting methanol to dimethylether;iii. a third ...

Recycle catalytic reforming process to increase aromatics yield

The invention relates to a process and system arrangement to generate benzene, toluene and xylenes in a refinery. The process relies on recycling a C9+ aromatic bottoms stream from an aromatic recovery complex back to rejoining a hydrotreated naphtha stream as it enters a catalytic reformer. The aromatic bottoms can be further reacted through both the reformer and the subsequent aromatic recovery complex to transform to higher value compounds, thereby reducing waste or reducing bottoms' presence in gasoline pools.

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 ...

A Naphtha Reforming Process

The present disclosure relates to a naphtha reforming process for obtaining reformed naphtha comprising contacting naphtha with a catalyst, the catalyst comprising a chloride free zeolite coated alumina support impregnated with 0.01 wt % to 0.5 wt % active metal and 0.01 wt % to 0.5 wt % promoter metal, wherein the thickness of the zeolite coating on the alumina support ranges from 100 μm to 200 μm, which results in formation of reformed products of naphtha and ethylbenzene formed in-situ. 1. A naphtha reforming process for obtaining reformed naphtha comprising contacting naphtha with a catalyst , said catalyst comprising a chloride free zeolite coated alumina support impregnated with 0.01 wt % to 0.5 wt % active metal and 0.01 wt % to 0.5 wt % promoter metal , wherein the thickness of the zeolite coating on the alumina support ranges from 100 μm to 200 μm , which results in formation of reformed products of naphtha and ethylbenzene formed in-situ.2. The naphtha reforming process as claimed in claim 1 , wherein said in-situ ethylbenzene is dealkylated into benzene (C) and/or toluene (C).3. The naphtha reforming process as claimed in claim 1 , wherein the ethylbenzene formed in the reformed products is in the range of 3.6 wt % to 4.75 wt % of the mass of the reformed products.4. The naphtha reforming process as claimed in claim 1 , wherein the ethylbenzene formed in the reformed products is in the range of 4.68% to 4.75% of the mass of the reformed products The present disclosure relates to a naphtha reforming process.An active metal is a Group VIII metal of the modern periodic table. The Group VIII metals are platinum (Pt), palladium (Pd) and nickel (Ni),A promoter metal is a Group IV metal of the modern periodic table. The Group IV metals are tin (Sn), rhenium (Re) and iridium (Ir).ZSM-5 is an aluminosilicate zeolite belonging to the pentasil family of zeolites and its chemical formula is NaAlSiO.16HO (0 Подробнее

MOLECULAR SIEVES AND A PROCESS FOR MAKING MOLECULAR SIEVES

Processes are provided for preparing molecular sieves. The process involves preparing a synthesis mixture for the molecular sieve wherein the synthesis mixture includes a morphology modifier L selected from the group consisting of nonionic surfactants, anionic surfactants, sugars and combinations thereof. 2) A process as claimed in in which in step a) one or more further components selected from the group consisting of a source of hydroxide ions claim 1 , a structure directing agent Q claim 1 , a source of a trivalent element Y claim 1 , a source of a pentavalent element Z claim 1 , a source of halide ions W claim 1 , a source of alkali metal ions M and/or a source of alkaline earth metal cations M claim 1 , are also combined into the synthesis mixture.3) A process as claimed in in which the molar ratio L:X in the synthesis mixture is in the range of from 0.001 to 0.03.4) A process as claimed in in which a source of a trivalent element Y is present in the synthesis mixture and Y is Al claim 1 , and the ratio of XO:YOis in the range of from 5 to 500.5) A process as claimed in in which the ratio Q:(XO+YO+ZO) is in the range of from 0.01 to 1.0.6) A process as claimed in in which the morphology modifier L is a monosaccharide.7) A process as claimed in in which the morphology modifier L is an anionic surfactant.8) A process as claimed in in which the anionic surfactant is an alkyl sulphate.9) A process as claimed in in which the alkyl sulphate is a C8 to C30 alkyl sulphate.10) A process as claimed in in which the morphology modifier L is a nonionic surfactant.11) A process as claimed in in which the non-ionic surfactant is a block copolymer comprising one or more blocks derived from ethylene oxide and one or more blocks derived from propylene oxide.12) A process as claimed in in which the synthesis mixture is substantially free of water-insoluble liquid components.13) A process as claimed in which includes the step of calcining the crystals recovered in step c) to give ...

MOLECULAR SIEVES AND A PROCESS FOR MAKING MOLECULAR SIEVES

Processes are provided for preparing molecular sieves of framework structure MEI, TON, MRE, MWW, MFS, MOR, FAU, EMT, or MSE. The process involves preparing a synthesis mixture for the molecular sieve wherein the synthesis mixture includes a morphology modifier L selected from the group consisting of cationic surfactants having a quaternary ammonium group comprising at least one hydrocarbyl group having at least 12 carbon atoms, nonionic surfactants, anionic surfactants, sugars and combinations thereof. 1) A process of preparing crystals of a molecular sieve having a framework code selected from the group consisting of MEI , TON , MRE , MWW , MFS , MOR , FAU , EMT , and MSE , the process comprising the steps of:a. combining at least a source of a tetravalent element X, a morphology modifier L, and water to form a synthesis mixture;b. heating said synthesis mixture under crystallization conditions for a time of about 1 hour to 100 days to form the crystals of the molecular sieve; andc. recovering said crystals of the molecular sieve from the synthesis mixture,wherein X=Si and the morphology modifier L is selected from the group consisting of cationic surfactants having a quaternary ammonium group comprising at least one hydrocarbyl group having at least 12 carbon atoms, nonionic surfactants, anionic surfactants, sugars and combinations thereof, and if a structure directing agent Q is present L is different from and is present in addition to the structure directing agent Q.2) A process as claimed in in which in step a) one or more further components selected from the group consisting of a source of hydroxide ions claim 1 , a structure directing agent Q claim 1 , a source of a trivalent element Y claim 1 , a source of a pentavalent element Z claim 1 , a source of halide ions W claim 1 , and a source of alkali metal ions M and/or a source of alkali earth metal cations M claim 1 , are also combined into the synthesis mixture.3) A process as claimed in in which the molar ...

PROCESS FOR MAKING MOLECULAR SIEVES

Processes are provided for preparing molecular sieves for use as catalysts. The process involves preparing a synthesis mixture for the molecular sieve wherein the synthesis mixture includes a morphology modifier which may be selected from cationic surfactants having a single quaternary ammonium group comprising at least one hydrocarbyl group having at least 12 carbon atoms, nonionic surfactants, anionic surfactants, sugars, and combinations thereof. 1) A process of preparing crystals of a molecular sieve , the process comprising the steps of:a. combining at least a source of a tetravalent element X, a morphology modifier L, and water to form a synthesis mixture;b. heating said synthesis mixture under crystallization conditions for a time of about 1 hour to 100 days to form the crystals of the molecular sieve; andc. recovering said crystals of the molecular sieve from the synthesis mixture;wherein the morphology modifier L is selected from the group consisting of cationic surfactants having a single quaternary ammonium group comprising at least one hydrocarbyl group having at least 12 carbon atoms, nonionic surfactants, anionic surfactants, sugars and combinations thereof, and is present in the synthesis mixture before nucleation or crystallization of the crystals begins;wherein if the molecular sieve is one which requires a structure directing agent Q, the morphology modifier L is different from and is present in addition to the structure directing agent Q;wherein the molar ratio L:X in the synthesis mixture is in the range of from 0.0001 to 0.03; andwherein the synthesis mixture is a liquid, or a mixture of solid and liquid, and the liquid is substantially a single phase.2) A process as claimed in claim 1 , wherein in step a) one or more further components selected from the group consisting of a source of hydroxide ions claim 1 , a structure directing agent Q claim 1 , a source of a trivalent element Y claim 1 , a source of a pentavalent element Z claim 1 , a ...

MANUFACTURING A BASE STOCK FROM ETHANOL

A systems and method for manufacturing a base stock from an ethanol stream are described herein. An example method includes dehydrating an ethanol stream to form an impure ethylene mixture, recovering an ethylene stream from the impure ethylene mixture, and oligomerizing the ethylene stream to form a raw oligomer stream. A heavy olefinic stream is distilled from the raw oligomer stream. The heavy olefinic stream is hydro-processed to form a hydro-processed stream, and the hydro-processed stream is distilled to form the base stock. 1. A system for manufacturing a base stock from an ethanol stream , comprising:a dehydration reactor configured to form an impure ethylene stream from the ethanol stream;a recovery system configured to purify the impure ethylene stream to form an ethylene stream;an oligomerization reactor configured to oligomerize the ethylene stream to form an oligomer stream; a light olefinic stream for recovery of linear alpha-olefins;', 'an intermediate olefinic stream; and', 'a heavy olefinic stream;, 'a distillation column configured to separate the oligomer stream intoa hydro-processing reactor configured to hydro-process the heavy olefinic stream to form a hydro-processed stream; anda product distillation column configured to separate the hydro-processed stream to form the base stock.2. The system of claim 1 , comprising a dimerization reactor configured to dimerize the intermediate olefinic stream and return a dimerized stream to the distillation column.3. The system of claim 1 , comprising an alkylation reactor configured to alkylate the intermediate olefinic stream and provide an alkylated stream to an alkylation distillation column.4. The system of claim 3 , wherein the alkylation distillation column is configured to separate an unreacted olefin stream from the alkylated stream and return the unreacted olefin stream to the alkylation reactor.5. The system of claim 1 , comprising a bioreactor to generate the ethanol stream.6. The system of claim ...

CATALYST WITH IMPROVED ACTIVITY/SELECTIVITY FOR LIGHT NAPHTHA AROMATIZATION

In an embodiment, A catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the catalyst has an Si:Almole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5; wherein the catalyst has an aluminum content of less than or equal to 0.75 wt %; wherein the catalyst is non-acidic. 1. A catalyst comprising:a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the zeolite is a medium pore zeolite having an average pore size of 5 to 8 Å;{'sub': '2', 'wherein the catalyst has an Si:Almole ratio of 125 to 211, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5;'}wherein the catalyst has an aluminum content of less than or equal to 0.75 wt %, and a Ge content of 0.1 to 3 wt %, based on the total weight of the catalyst excluding any binder and extrusion aide;wherein the catalyst is non-acidic.2. The catalyst of claim 1 , wherein the Ge is present in an amount of 0.4 to 2.5 wt % claim 1 , and/or the Na is present in an amount of 0.5 to 2 wt % and/or the Pt is present in an amount of 0.05 to 3 wt % claim 1 , wherein the wt % values are based on the total weight of the catalyst excluding any binder and extrusion aide.3. The catalyst of claim 2 , wherein the catalyst has all of the Ge content of 0.4 to 2.5 wt % claim 2 , the Na content of 0.5 to 2 wt % claim 2 , and the Pt content of 0.05 to 3 wt % claim 2 , wherein the wt % values are based on the total weight of the catalyst excluding any binder and extrusion aide.4. The catalyst of claim 1 , wherein the catalyst has a Ge content of 0.4 to 1.5 wt % based on the total weight of the catalyst excluding any binder and extrusion aide.5. The catalyst of claim 1 , wherein the catalyst comprises Al in an amount of 0.45 to 0.7 wt % based on the total weight of the catalyst excluding any binder and extrusion aide.6. The catalyst of claim 1 , wherein the zeolite is MTW claim 1 , ...

A Process For Preparing A Catalyst

The present disclosure relates to a process for preparing a catalyst. The process comprises coating zeolite gel over the alumina support to obtain a chloride free zeolite gel coated alumina support, crystallizing the chloride free zeolite gel coated alumina support, washing, drying and calcining the crystallized zeolite coated alumina support to obtain a calcined crystallized chloride free zeolite coated alumina support, treating the calcined crystallized chloride free zeolite coated alumina support with ammonium nitrate to obtain sodium free support, washing, drying, and calcining the support to obtain a calcined chloride free zeolite coated alumina support, immersing the calcined chloride free zeolite coated alumina support in an active metal and a promoter metal solution mixture followed by stirring to obtain a metal coated chloride free zeolite coated alumina support, and drying and calcining the metal coated chloride free zeolite coated alumina support to obtain the catalyst. 1. A process for preparing a catalyst comprising the following steps:a) providing alumina support;b) coating zeolite gel over the alumina support to obtain a chloride free zeolite gel coated alumina support;c) crystallizing the chloride free zeolite gel coated alumina support to obtain a crystallized zeolite coated alumina support;d) washing, drying and calcining the crystallized chloride free zeolite coated alumina support to obtain a calcined crystallized chloride free zeolite coated alumina support;e) treating the calcined crystallized chloride free zeolite coated alumina support with ammonium nitrate to obtain sodium free support; andf) washing, drying, and calcining the support to obtain a calcined chloride free zeolite coated alumina support.g) immersing the calcined chloride free zeolite coated alumina support in an active metal and a promoter metal solution mixture followed by stirring to obtain a metal coated chloride free zeolite coated alumina support; andh) drying and calcining ...

HIGH CHARGE DENSITY METALLOALUMINOPHOSPHOSILICATE MOLECULAR SIEVES MeAPSO-82

A new family of crystalline microporous metalloalumino(gallo)phosphosilicates designated MeAPSO-82 has been synthesized. These metalloalumino(gallo)phosphosilicates are represented by the empirical formula of: R p+ r A + m M 2+ w E x PSi y O z where A is an alkali metal such as potassium, R is an quaternary ammonium cation such as ethyltrimethylammonium, M is a divalent metal such as Zn and E is a trivalent framework element such as aluminum or gallium. This family of metalloalumino(gallo)phosphosilicate materials are stabilized by combinations of alkali and quaternary ammonium cations, enabling unique, high charge density compositions. The MeAPSO-82 family of materials have the CGS topology and have catalytic properties for carrying out various hydrocarbon conversion processes and separation properties for separating at least one component.

Catalyst Composition For Converting Light Naphtha To Aromatic Compounds And A Process Thereof

Accordingly, the present invention provides a catalyst composition suitable for converting light naphtha comprising one or more of C5 to C8 carbon atoms to aromatic compounds ranging from C6 to C10 carbon atoms, said catalyst composition comprising: (a) a medium pore size zeolite; (b) 0.1 to 5.0 wt % of zinc; and (c) 0.1 to 5 wt % of gallium. Also, the present invention provides a process for converting light naphtha comprising one or more of C5 to C8 carbon atoms to aromatic compounds ranging from C6 to C10 carbon atoms, said process comprising the step of contacting a feedstock comprising the light naphtha with a catalyst composition comprising (a) a medium pore size zeolite; (b) 0.1 to 5.0 wt % of zinc; and (c) 0.1 to 5 wt % of gallium in presence of carrier gas at temperatures ranging from 400° to 600° C. 1. A catalyst composition suitable for converting light naphtha comprising one or more of C5 to C8 carbon atoms to aromatic compounds ranging from C6 to C10 carbon atoms , said catalyst composition comprising: (a) a medium pore size zeolite; (b) 0.1 to 5.0 wt % of zinc and (c) 0.1 to 5 wt % of gallium.2. The catalyst composition as claimed in claim 1 , wherein the medium pore size zeolite is hydrogen form medium pore alumino silicate zeolite.3. The catalyst composition as claimed in claim 1 , wherein the hydrogen form medium pore alumino silicate zeolite has silica to alumina ratio (SAR) in the range of 20 to 200.4. The catalyst composition as claimed in claim 1 , wherein the medium pore size zeolite is hydrogen form medium pore gallium molecular sieve.5. The catalyst composition as claimed in claim 1 , wherein the catalyst composition optionally further comprises one or more optional promoters selected from the group comprising of Cerium claim 1 , Chromium claim 1 , Tin claim 1 , Cesium claim 1 , potassium claim 1 , magnesium claim 1 , molybdenum and mixtures thereof.6. The catalyst composition as claimed in claim 5 , wherein the one or more optional promotes ...

PROCESS FOR REDUCING THE BENZENE CONTENT OF GASOLINE

A process is described for reducing the level of benzene in a refinery gasoline feed containing benzene and at least one C olefin, in which the refinery gasoline feed is contacted with a first alkylation catalyst under conditions effective to react at least part of the C olefin and benzene in the refinery gasoline feed and produce a first alkylation effluent. The first alkylation effluent is separated into at least (i) a first fraction rich in benzene, (ii) a second fraction rich in Cto Chydrocarbons and (iii) a third fraction rich in C hydrocarbons. At least part of the first fraction is contacted with an alkylating agent comprising one or more Cto Colefins in the presence of a second alkylation catalyst under conditions effective to produce a second alkylation effluent which has reduced benzene content as compared with the first fraction. 1. A process for reducing the level of benzene in a refinery gasoline feed containing benzene and at least one C olefin , said process comprising:{'sub': '5+', '(a) contacting the refinery gasoline feed with a first alkylation catalyst under conditions effective to react at least part of the C olefin and benzene in the refinery gasoline feed and produce a first alkylation effluent;'}{'sub': 7', '12', '13+, '(b) separating the first alkylation effluent into at least (i) a first fraction rich in benzene, (ii) a second fraction rich in Cto Chydrocarbons and (iii) a third fraction rich in C hydrocarbons; and'}{'sub': 2', '4, '(c) contacting at least part of the first fraction with an alkylating agent comprising one or more Cto Colefins in the presence of a second alkylation catalyst under conditions effective to produce a second alkylation effluent which has reduced benzene content as compared with the first fraction.'}2. A process according to claim 1 , wherein the refinery gasoline feed has a boiling range at atmospheric pressure from 0° C. to 250° C.3. A process according to claim 1 , wherein the refinery gasoline feed is a ...

Method of Manufacturing a Reforming Fuel by Adding Water to a Fuel Oil and the Manufacturing Apparatus thereof

A method of manufacturing a reforming fuel by adding water to a fuel oil and a manufacturing apparatus is provided, the method and the apparatus comprising of preprocessing water in a water tank, aerating the water simultaneously in the water tank using the air previously processed by passing through ceramic catalyst, passing the water to an ultrasonic and electric field chamber, preprocessing fuel oil in a fuel oil tank with the catalyst, mixing the pre-processed water and fuel oil in a mixing chamber to produce a reforming fuel oil and passing the reforming fuel oil through one or a plurality of combination chambers.

NAPHTHA REFORMING CATALYST AND PROCESSES THEREOF

The present invention provides catalyst comprising metal modified zeolite, particularly Group IIIA or Group IIB metal modified zeolite, or a Group IIIA metal and Group IIB metal modified zeolite for reforming of heart cut naphtha stream. The present disclosure also relates to a process for synthesis of the catalyst. The present disclosure further relates to a process for reforming of heart cut naphtha stream, with high selectivity towards aromatics and good activity using the catalytic system, in the absence of hydrogen. 1: A naphtha reforming catalyst comprising metal , zeolite and binder , wherein the metal is selected from Group IIIA metal , Group IIB metal or combination thereof.2: A process for preparing naphtha reforming catalyst comprising metal , zeolite and binder , wherein metal is selected from Group IIIA metal , Group IIB metal or combination thereof , said process comprising acts of:a) adding binder source to zeolite or adding metal to zeolite followed by binder source, optionally along with reagent to obtain extruder;b) drying and calcining the extruder to obtain calcined extruder;c) crushing the calcined extruder to obtain powder;d) optionally loading metal onto the powder to obtain metal loaded powder; ande) drying and calcining the metal loaded powder to obtain the catalyst.3: The process as claimed in claim 2 , wherein prior to adding the binder source or the metal to the zeolite claim 2 , the zeolite is calcined at temperature ranging from about 500° C. to about 550° C. claim 2 , preferably about 550° C. for time period ranging from about 10 hours to about 18 hours claim 2 , preferably about 15 hours; wherein the binder source is selected from group comprising Pseudoboehmite claim 2 , aluminum hydroxide claim 2 , aluminum sulphate and aluminum chloride claim 2 , preferably Pseudoboehmite; wherein the reagent is selected from alcohol and acid claim 2 , wherein the alcohol is polyvinyl alcohol and wherein the acid is selected from acetic acid and ...

Aromatization Catalyst Preparation with Alkali Metal Present During a Washing Step

Methods for producing supported catalysts containing a transition metal and a bound zeolite base are disclosed. These methods employ a step of washing the bound zeolite base in the presence of an alkali metal, prior to impregnating the bound zeolitic support with the transition metal. Alkali metals such as potassium and cesium may be used. 1. A method of producing a supported catalyst , the method comprising:(a) providing a bound zeolite base;(b) washing the bound zeolite base with an aqueous solution comprising cesium to produce a cesium enriched zeolite support; and(c) impregnating the cesium enriched zeolite support with a transition metal and a halogen to produce the supported catalyst;wherein the concentration of cesium in the aqueous solution is in a range from about 0.01 M to about 5 M.2. The method of claim 1 , wherein:the bound zeolite base comprises a silica-bound K/L-zeolite;the transition metal comprises platinum; andthe halogen comprises chlorine, fluorine, or both.3. The method of claim 1 , wherein:the aqueous solution further comprises potassium, rubidium, or a combination thereof; andthe supported catalyst comprises from about 5 wt. % to about 30 wt. % of a binder, based on the total weight of the supported catalyst.4. The method of claim 1 , wherein the supported catalyst comprises:from about 0.2 wt. % to about 5 wt. % transition metal;from about 0.2 wt. % to about 3 wt. % halogen; andfrom about 2 wt. % to about 10 wt. % cesium;based on the total weight of the supported catalyst.5. The method of claim 1 , wherein step (b) comprises from 2 to 8 washing cycles claim 1 , each washing cycle conducted independently at a washing temperature in a range from about 20° C. to about 95° C. and for a time period in a range from about 5 minutes to about 2 hours.6. The method of claim 5 , wherein a ratio of the weight of the aqueous solution to the weight of the bound zeolite base in each washing cycle independently is in a range about 0.4:1 to about 10:1.7. The ...

Hydrocarbon aromatization catalyst composition and method of formation

A method for forming a catalyst can comprise: heating a Ge-ZSM-5 zeolite powder at a temperature of 400 to 600° C.; ion-exchanging the heat-treated zeolite powder with an alkali metal and impregnating the heat-treated zeolite powder with noble metal; heating the ion-exchanged, impregnated zeolite powder to a temperature of 250 to 350° C.; mixing the second heat-treated zeolite powder with a solid silica binder and a colloidal silica binder to form a mixture, wherein if the solid silica has a purity of less than or equal to 66 wt % of silica oxide based on the total weight of the solid silica, then the mixture is free of an extrusion aide and the colloidal silica has a particle size of less than 20 nm as measured along a major axis; forming the mixture into a shaped body; and heating the shaped body to 100 to 350° C. to result in the catalyst.

Zeolite catalysts, methods for producing zeolite catalysts, and methods for producing lower olefins

Provided are zeolite catalysts that allow reactions to proceed at temperatures as low as possible when lower olefins are produced from hydrocarbon feedstocks with low boiling points such as light naphtha, make it possible to make propylene yield higher than ethylene yield in the production of lower olefins, and have long lifetime. The zeolite catalysts are used in the production of lower olefins from hydrocarbon feedstocks with low boiling points such as light naphtha. The zeolite catalysts are MFI-type crystalline aluminosilicates containing iron atoms and have molar ratios of iron atoms to total moles of iron atoms and aluminum atoms in the range from 0.4 to 0.7. The use of the zeolite catalysts make it possible to increase propylene yield, to lower reaction temperatures, and to extend catalyst lifetime.

Process For Enhancement Of RON Of FCC Gasoline With Simultaneous Reduction In Benzene

The present invention relates to an integrated process for increasing the research octane number (RON) of FCC gasoline with simultaneous reduction in benzene content. In this process, benzene rich gasoline fraction is reacted with light olefin rich gaseous streams like FCC off gas/dry gas, coker off gas to produce alkyl aromatics using FCC catalyst system containing ZSM-5 zeolite. The catalyst is continuously drawn from the FCC regenerator by suitably placing the alkylation reactor in communication with the FCC regenerator. The product stream of the alkylation reactor is routed to main fractionator for separation of off gas and benzene lean gasoline. This integrated process not only improves the octane number of gasoline but also lowers the gasoline benzene content. Further the integrated alkylation reactor system acts as a heat sink lowering the FCC regenerator temperature and enables the FCC unit to process high CCR feeds. 1. An integrated process for increasing the research octane number (RON) of gasoline and simultaneous reduction in its benzene content , said process comprising:contacting benzene rich gasoline fraction with light olefin rich stream in a fluidized bed alkylation reactor with FCC catalyst to produce alkyl aromatics, wherein the FCC catalyst is continuously drawn from the FCC regenerator, which is in communication with alkylation reactor, whereby stream from alkylation reactor is separated into off gas and benzene lean gasoline.2. The process as claimed in claim 1 , wherein the catalyst system comprises of two components; FCC catalyst comprising of Y-type Zeolite claim 1 , an active alumina material claim 1 , a binder material claim 1 , comprising either silica or alumina or combination thereof and an inert filler such as kaolin claim 1 , and medium or smaller pore zeolite based additive.3. The process as claimed in claim 1 , wherein FCC catalyst system contains 5-50 wt % of ZSM-5 additive.4. The process as claimed in claim 1 , wherein the ...

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 ...

METHOD FOR PRODUCING MONOCYCLIC AROMATIC HYDROCARBON HAVING 6 - 8 CARBON ATOMS

A method for producing a monocyclic aromatic hydrocarbon having 6 to 8 carbon atoms, including bringing a raw material which contains a light hydrocarbon having 2 to 7 carbon atoms as a main component into contact with a catalyst composition for producing a monocyclic aromatic hydrocarbon having 6 to 8 carbon atoms. The catalyst composition for producing a monocyclic aromatic hydrocarbon having 6 to 8 carbon atoms is coated with an amorphous silicon oxide compound and contains a crystalline aluminosilicate, and the silicon oxide compound is a silicon oxide compound derived from a compound represented by XSi(OR), where X represents a hydrogen atom or an alkyl group, R represents an alkyl group, and n represents an integer of 0 to 4. 1. A method for producing a monocyclic aromatic hydrocarbon having 6 to 8 carbon atoms , the method comprising:bringing a raw material which contains a light hydrocarbon having 2 to 7 carbon atoms as a main component into contact with a catalyst composition for producing a monocyclic aromatic hydrocarbon having 6 to 8 carbon atoms,wherein the catalyst composition for producing a monocyclic aromatic hydrocarbon having 6 to 8 carbon atoms is coated with an amorphous silicon oxide compound and contains a crystalline aluminosilicate, and {'br': None, 'sub': n', '4-n, 'XSi(OR)\u2003\u2003(1)'}, 'the silicon oxide compound is a silicon oxide compound derived from a compound represented by Formula (1),'}wherein X represents a hydrogen atom or an alkyl group, R represents an alkyl group, and n represents an integer of 0 to 4.2. The method for producing a monocyclic aromatic hydrocarbon having 6 to 8 carbon atoms according to claim 1 , wherein a molar ratio of an acid quantity of the catalyst composition to Al is 1.25 or less claim 1 , the acid quantity being defined by an amount of ammonia desorbed in a temperature range of 200° C. to 500° C. in an NH-TPD method.3. The method for producing a monocyclic aromatic hydrocarbon having 6 to 8 carbon ...

SINGLE-LOOP OCTANE ENRICHMENT

The present invention provides apparatuses and processes for producing high octane fuel from synthesis gas. The process combines transalkylation and zeolite-forming/aromatization in conjunction with a single recycle loop configuration in order to effectively promote the fuel quality, particularly octane rating. The process involves adding a step for enriching octane of the fuel coming from the single recycle loop process. Preferably, the enrichment step takes place in an octane enrichment reactor containing two different catalysts, a zeolite-forming/aromatization catalyst followed by a transalkylation catalyst. The final fuel product preferably has an octane of about 92 to about 112. 1. A process for producing a high octane fuel comprising the step of passing a feed stream containing a medium octane fuel through an octane enrichment reactor containing a zeolite forming catalyst and a transalkylation catalyst.2. The process of wherein the medium octane fuel is produced byi. passing the synthesis gas to convert synthesis gas to methanol and water, which produces a first exit through a first reactor stream;ii. passing the first exit stream through a second reactor to convert methanol to dimethylether, which produces a second exit stream;iii. passing the second exit stream through a third reactor to convert methanol and dimethylether to fuel and heavy gasoline, which produces a third exit stream;iv. passing the third exit stream through a fourth reactor to convert the heavy gasoline to isoparaffins, naphthenes, and less substituted aromatics, which produces a fourth exit stream;v. passing the fourth exit stream through a condenser to separate unreacted synthesis gas from the medium octane fuel; andvi. recycling the unreacted synthesis gas to the first reactor; wherein no removal or separation of the first, second or third exit streams are effected during steps a) to d).3. The process of wherein the medium octane fuel is produced byi. passing the synthesis gas through a ...

Selective Poisoning of Aromatization Catalysts to Increase Catalyst Activity and Selectivity

Spent aromatization catalysts containing a transition metal and a catalyst support are selectively poisoned in the disclosed reforming methods, resulting in improvements in overall aromatics yield and selectivity.

IMPROVED PROCESS FOR CATALYST ACTIVATION FOR LOWER ALKANE DEHYDROAROMATIZATION

Described herein is a method for producing a zeolite catalyst useful for aromatization of a lower alkane, a zeolite catalyst useful for aromatization of a lower alkane obtainable by said method and a process for aromatization of a lower alkane using the zeolite catalyst. 1. A method for producing a zeolite catalyst useful for aromatization of a lower alkane comprising:contacting a molybdenum modified zeolite catalyst precursor with a gas stream comprising a lower alkane and a reducing gas at a first temperature of 40° C. to 250° C. that is increased to a second temperature of greater than 250° C. to 750° C. at a rate of less than or equal to 5° C./min to yield an activated zeolite catalyst.2. The method of claim 1 , wherein the temperature increases at a rate less than or equal to 3° C./min.3. The method of claim 1 , wherein the temperature increases at a rate of less than or equal to 2° C./min.4. The method of claim 1 , wherein the gas stream comprises 5 vol. % to 30 vol. % of the lower alkane.5. The method of claim 1 , wherein the lower alkane comprises methane.6. The method of claim 1 , wherein the molybdenum modified zeolite catalyst precursor comprises H-ZSM-5.7. The method of claim 1 , wherein the molybdenum modified zeolite catalyst precursor further comprises 0.1 wt. % to 2 wt. % of an additional element selected from the Groups 6-11 of the Periodic Table.8. The method of claim 1 , wherein the reducing gas comprises hydrogen.9. The method of claim 1 , wherein the gas stream comprises 70-95 vol. % of the reducing gas.10. The method of claim 1 , wherein the first temperature is from 50 to 70° C. claim 1 , the second temperature is 600 to 700° C. claim 1 , and the rate is 1° C./min to 3° C./min.11. The method of claim 1 , wherein the gas activated zeolite catalyst has a Si/Al ratio of 10 to 20 claim 1 , or claim 1 , 11 to 18.12. The method of claim 1 , wherein an inert gas is present in an amount less than or equal to 10 vol. % claim 1 , based on the total ...

Aromatization Processes Using Both Fresh and Regenerated Catalysts, and Related Multi-Reactor Systems

Multi-reactor systems with aromatization reactor vessels containing a catalyst with low surface area and pore volume, followed in series by aromatization reactor vessels containing a catalyst with high surface area and pore volume, are disclosed. Related reforming methods using the different aromatization catalysts also are described. 111-. (canceled)12. An aromatization reactor vessel system comprising:(A) at least one first reactor vessel comprising:(a1) a first reactor inlet for introducing a first hydrocarbon feed into the at least one first reactor vessel;(a2) a first aromatization catalyst for catalytically converting at least a portion of the first hydrocarbon feed under first reforming conditions to produce a first aromatic product; wherein the first aromatization catalyst comprises a first transition metal and a first catalyst support, the first aromatization catalyst characterized by:{'sup': 2', '2, 'a first surface area in a range from about 80 m/g to about 150 m/g; and/or'}a first micropore volume in a range from about 0.01 cc/g to about 0.048 cc/g; and(a3) a first reactor outlet for discharging a first effluent comprising the first aromatic product from the at least one first reactor vessel;(B) at least one second reactor vessel comprising:(b1) a second reactor inlet for introducing a second hydrocarbon feed into the at least one second reactor vessel;(b2) a second aromatization catalyst for catalytically converting at least a portion of the second hydrocarbon feed under second reforming conditions to produce a second aromatic product; wherein the second aromatization catalyst comprises a second transition metal and a second catalyst support, the second aromatization catalyst characterized by:{'sup': 2', '2, 'a second surface area in a range from about 160 m/g to about 260 m/g; and/or'}a second micropore volume in a range from about 0.05 cc/g to about 0.09 cc/g; and(b3) a second reactor outlet for discharging a second effluent comprising the second ...

Methods of Regenerating Aromatization Catalysts with A Decoking Step Between Chlorine and Fluorine Addition

Methods for regenerating a spent catalyst are disclosed. Such methods may employ a step of chlorinating the spent catalyst in the gas phase, followed by decoking the chlorinated spent catalyst, and then fluorinating the de-coked catalyst in a fluorine-containing solution of a fluorine-containing compound. 122-. (canceled)23. A method for regenerating a chlorinated spent catalyst comprising a transition metal and a catalyst support , the method comprising:(i) contacting the chlorinated spent catalyst with a decoking gas stream comprising oxygen to produce a de-coked chlorinated catalyst,wherein the chlorinated spent catalyst comprises from about 0.5 wt. % to about 3 wt. % of chlorine; and(ii) contacting the de-coked chlorinated catalyst with a fluorine-containing solution comprising a fluorine-containing compound in the liquid phase to produce a fluorinated catalyst; wherein:the transition metal comprises a Group 8-11 transition metal; andthe catalyst support comprises a large pore zeolite having an average pore diameter in a range of from about 7 Å to about 12 Å.24. The method of claim 23 , wherein the chlorinated spent catalyst further comprises fluorine.25. The method of claim 23 , wherein the chlorinated spent catalyst comprises at least about 1 wt. % carbon.26. The method of claim 23 , wherein the de-coked chlorinated catalyst comprises less than about 0.5 wt. % carbon.27. The method of claim 23 , wherein:step (i) is conducted at a peak decoking temperature in a range from about 300° C. to about 500° C.;the decoking gas stream comprises an inert gas and oxygen; andthe decoking gas stream is substantially free of halogen-containing compounds.28. The method of claim 23 , wherein an amount of the fluorine-containing compound in the fluorine-containing solution provides from about 0.1 to about 10 wt. % of fluorine (F) in the fluorine-containing solution.29. The method of claim 23 , wherein:step (ii) is conducted at a fluorination temperature in a range from about 20 ...

Aromatization Processes Using Both Fresh and Regenerated Catalysts, and Related Multi-Reactor Systems

Multi-reactor systems with aromatization reactor vessels containing a catalyst with low surface area and pore volume, followed in series by aromatization reactor vessels containing a catalyst with high surface area and pore volume, are disclosed. Related reforming methods using the different aromatization catalysts also are described.

Catalyst composite for the reduction of olefins in the fcc naphtha stream

The present disclosure relates to a catalyst composition comprising (a) at least one rare earth metal, (b) at least one zeolite, and (c) at least one diluent, wherein, said rare earth metal is impregnated in at least one of (b) and (c); the ratio of said zeolite to said diluent ranges from 1:9 to 9:1; and the amount of said rare earth metal is in the range of 0.1 to 20 w/w %. The present disclosure also relates to a process for preparing a catalyst composition. Further, the present disclosure relates to a process for reducing the olefin content in a hydrocarbon stream using the catalyst of the present disclosure.

ZEOLITE BASED CATALYST COMPOSITION FOR THE REDUCTION OF OLEFINS IN FCC NAPHTHA

The present disclosure relates to a zeolite based catalyst composition comprising i. at least one rare earth metal, ii. at least one zeolite, and iii. optionally, at least one promoter; wherein, said rare earth metal is impregnated in said zeolite. The amount of said rare earth metal in said composition is in the range of 0.1 to 20 w/w %. The present disclosure also relates to a process for preparing a catalyst composition. Further, the present disclosure relates to a process for reducing olefin content in a hydrocarbon stream using the catalyst of the present disclosure. 1. A zeolite based catalyst composition comprising:a. at least one rare earth metal; andb. at least one zeolite,wherein, the amount of said rare earth metal is in the range of 0.1 to 20 w/w %.2. The catalyst composition as claimed in claim 1 , wherein said rare earth metal is impregnated in said zeolite.3. The catalyst composition as claimed in claim 1 , wherein the ratio of SiOto AlOin said zeolite ranges from 1:20 to 1:450.4. The catalyst composition as claimed in claim 1 , wherein the rare earth metal is selected from the group consisting of scandium claim 1 , yttrium claim 1 , lanthanum claim 1 , praseodymium claim 1 , neodymium claim 1 , promethium claim 1 , samarium claim 1 , europium claim 1 , gadolinium claim 1 , terbium claim 1 , dysprosium claim 1 , holmium claim 1 , erbium claim 1 , thulium claim 1 , ytterbium and lutetium and said metal is in a salt form selected from the group consisting of chloride claim 1 , bromide claim 1 , fluoride claim 1 , iodide claim 1 , sulfates claim 1 , phosphates claim 1 , phosphonates claim 1 , nitrates claim 1 , nitrites claim 1 , carbonates claim 1 , acetates claim 1 , bicarbonates claim 1 , hydroxides and oxides.5. The catalyst composition as claimed in claim 1 , wherein the zeolite is selected from the group consisting of ZSM-5 claim 1 , ZSM-11 claim 1 , ZSM-12 claim 1 , ZSM-22 claim 1 , ZSM-23 claim 1 , ZSM-48 claim 1 , ZSM-57 claim 1 , SAPO-5 claim 1 ...

System and Method for On Stream Catalyst Replacement

A system of reforming reactors comprises a plurality of reactors coupled by flow lines, a feed header coupled to the plurality of reactors by a plurality of feed lines, an effluent header coupled to the plurality of reactors by a plurality of effluent lines, and a plurality of valves disposed in the flow lines, the feed lines, and the effluent lines. Each reactor comprises a reforming catalyst, and the plurality of valves are capable of being dynamically operated to create a first serial flow path through the plurality of reactors. The plurality of valves is further configured to dynamically reconnect the plurality of reactors to create a second serial flow path through the plurality of reactors. A first reactor of the plurality of reactors is adjacent to a second reactor of the plurality of reactors in the first serial flow path, and the first reactor is not adjacent to the second reactor in the second serial flow path. 1. A system comprising:a plurality of reactors coupled by flow lines, wherein each reactor comprises a reforming catalyst;a feed header coupled to the plurality of reactors by a plurality of feed lines;an effluent header coupled to the plurality of reactors by a plurality of effluent lines; anda plurality of valves disposed in the flow lines, the feed lines, and the effluent lines,wherein the plurality of valves are capable of being dynamically operated to create a first serial flow path through the plurality of reactors, wherein a first reactor of the plurality of reactors is adjacent to a second reactor of the plurality of reactors in the first serial flow path,wherein the plurality of valves are further configured to dynamically reconnect the plurality of reactors to create a second serial flow path through the plurality of reactors, wherein the first reactor is not adjacent to the second reactor in the second serial flow path.2. The system of claim 1 , wherein the plurality of valves are further configured to bypass at least one reactor of the ...

Single step catalytic process for the conversion of n-paraffins and naphtha to diesel range hydrocarbons

The present invention discloses a single step catalytic process for the conversion of n-paraffins and naphtha to diesel range hydrocarbons. A bi-metallic Pt—Sn/ZSM-5 catalyst has been developed for the direct conversion of n-heptane as well as naphtha into diesel range hydrocarbons in a single step process.

Zeolite catalysts, methods for producing zeolite catalysts, and methods for producing lower olefins

Provided are zeolite catalysts that allow reactions to proceed at temperatures as low as possible when lower olefins are produced from hydrocarbon feedstocks with low boiling points such as light naphtha, make it possible to make propylene yield higher than ethylene yield in the production of lower olefins, and have long lifetime. The zeolite catalysts are used in the production of lower olefins from hydrocarbon feedstocks with low boiling points such as light naphtha. The zeolite catalysts are MFI-type crystalline aluminosilicates containing iron atoms and have molar ratios of iron atoms to total moles of iron atoms and aluminum atoms in the range from 0.4 to 0.7. The use of the zeolite catalysts make it possible to increase propylene yield, to lower reaction temperatures, and to extend catalyst lifetime.

A METHOD FOR PRODUCING HIGH-OCTANE MOTOR GASOLINES OF LOW-OCTANE HYDROCARBON FRACTIONS, FRACTIONS OF GASEOUS OLEFINS AND OXYGENATES AND A PLANT FOR THE METHOD EMBODIMENT

The invention relates to method and plant for the production of high-octane gasolines from raw hydrocarbon fractions, fractions of gaseous olefins and oxygenates. A method has been proposed, wherein the feedstock component flow is supplied to a unit for supplying flows to be treated, into the reactor, wherein the reaction is carried out in the presence of a zeolite-containing catalyst, high-octane gasoline is isolated by separation of the conversion product, while diverting simultaneously the reaction water and the exhaust gases. A reactor contains at least two reaction zones, between which there are further arranged means for mixing the reaction product from the previous reaction zone and the supplied oxygenates and olefin-containing feedstock, whereas using the unit for supplying flows there is supplied a flow oxygenates and olefin-containing feedstock and the flow of raw hydrocarbon fractions into the first reaction zone of the reactor, and the flow oxygenates and olefin-containing feedstock into the second reaction zone of the reactor.

Aromatization Catalysts With High Surface Area and Pore Volume

Regenerable aromatization catalysts having high surface area and pore volume, as well as methods for producing these catalysts, are disclosed. 113-. (canceled)14. A method of producing a catalyst , the method comprising:(a) contacting a zeolitic base with an alkaline earth metal-containing compound to form an alkaline earth metal exchanged zeolitic support;(b) calcining the alkaline earth metal exchanged zeolitic support at a peak calcining temperature of less than about 550° C. (1022° F.);(c) impregnating the calcined alkaline earth metal exchanged zeolitic support with a Group VIII transition metal-containing compound; and{'sup': '2', '(d) calcining the impregnated alkaline earth metal exchanged zeolitic support to produce a catalyst having a surface area of at least about 165 m/g.'}15. The method of claim 14 , wherein:the zeolitic base comprises a L-zeolite;the alkaline earth metal-containing compound comprises barium; andthe Group VIII transition metal-containing compound comprises platinum.16. The method of claim 15 , wherein step (a) is the only step in the method which utilizes a barium-containing compound.17. The method of claim 16 , wherein the peak calcining temperature in step (b) is in a range of from about 315° C. (600° F.) to about 538° C. (1000° F.).18. The method of claim 17 , wherein:the peak calcining temperature in step (b) is in a range of from about 399° C. (750° F.) to about 493° C. (920° F.); orthe method does not include a contacting step comprising a fluorine-containing compound; orthe method does not include a contacting step comprising a chlorine-containing compound other than the platinum-containing compound; orany combination thereof.19. A reforming process comprising:contacting a hydrocarbon feed with a supported aromatization catalyst under reforming conditions in a reactor system to produce an aromatic product; wherein the supported aromatization catalyst comprises:an alkaline earth metal exchanged zeolitic support; and(ii) a Group ...

METHOD OF PRODUCING LOWER OLEFIN AND MONOCYCLIC AROMATIC HYDROCARBON HAVING 6 TO 8 CARBON ATOMS AND DEVICE FOR PRODUCING LOWER OLEFIN AND MONOCYCLIC AROMATIC HYDROCARBON HAVING 6 TO 8 CARBON ATOMS

A method of producing a lower olefin and BTX from stock oils selected from at least two kinds of oils is provided. The method includes a first catalytic cracking step of bringing one stock oil A into contact with a catalytic cracking catalyst; a second catalytic cracking step of bringing one stock oil B, having an aromatic component content smaller than that of the stock oil A, into contact with the catalytic cracking catalyst; and a separation and collection step of collecting the lower olefins and BTX from a product generated in the first and second catalytic cracking steps. A contact time A during which the stock oil A is in contact with the catalytic cracking catalyst in the first catalytic cracking step is longer than a contact time B during which the stock oil B is in contact with the catalytic cracking catalyst in the second catalytic cracking step. 1. A method of producing a lower olefin and a monocyclic aromatic hydrocarbon having 6 to 8 carbon atoms from stock oils selected from at least two or more kinds of oils , the method comprising:a first catalytic cracking step of bringing one stock oil A among the stock oils into contact with a catalytic cracking catalyst;a second catalytic cracking step of bringing one stock oil B, having an aromatic component content smaller than that of the stock oil A, among the stock oils into contact with the catalytic cracking catalyst; anda separation and collection step of collecting the lower olefins and the monocyclic aromatic hydrocarbons having 6 to 8 carbon atoms from a product generated in the first and second catalytic cracking steps,wherein a contact time A during which the stock oil A is in contact with the catalytic cracking catalyst in the first catalytic cracking step is longer than a contact time B during which the stock oil B is in contact with the catalytic cracking catalyst in the second catalytic cracking step.2. The method of producing a lower olefin and a monocyclic aromatic hydrocarbon having 6 to 8 ...

Methods of Regenerating Aromatization Catalysts with a Decoking Step Between Chlorine and Fluorine Addition

Methods for regenerating a spent catalyst in a metal reactor are disclosed. Such methods may employ a step of chlorinating the spent catalyst, followed by decoking the chlorinated spent catalyst, and then fluorinating the de-coked catalyst.

NAPHTHA REFORMER YIELD USING MODIFIED ZEOLITIC CATALYSTS

This application relates to methods and systems for the conversion of hydrocarbon feedstocks, in particular, naphtha feedstocks, into a hydrocarbon product stream containing a high yield of high-octane gasoline and chemicals products. In particular, the conversion takes place over a series of functionally distinctive catalyst beds, at least one of which includes a modified zeolitic catalyst comprising a zeolite, a transition metal, and optionally a binder. Systems provided include a hydrocarbon feed stream, which may be full-range naphtha, a hydrocarbon product stream, and a plurality of functionally distinctive catalyst beds arranged in series, wherein at least one of the catalyst beds comprises a modified zeolitic catalyst. A hydrocarbon feed stream may be conveyed through the plurality of functionally distinctive catalyst beds, producing an intermediate hydrocarbon stream between each, under conditions effective to convert the hydrocarbon feed stream to a hydrocarbon product stream comprising high-octane gasoline, xylenes, benzene, and/or toluene 1. A system for converting hydrocarbons , wherein the system comprises:a hydrocarbon feed stream;an intermediate hydrocarbon feed stream comprising not more than about 34 wt. % naphthenes;a hydrocarbon product stream comprising at least one product selected from the group consisting of high-octane gasoline, xylenes, benzene, and toluene, and{'sub': '5+', 'wherein when the C fraction of the hydrocarbon product stream has a RON of 95, the Cs+fraction yield is at least 80 wt. %;'}a first functionally distinctive catalyst bed and a second functionally distinctive catalyst bed arranged in sequence, wherein at least one of the functionally distinctive catalyst beds is constructed and arranged to accept the intermediate feed stream and comprises a first modified zeolitic catalyst comprising a first modified zeolite, a first transition metal, and optionally a first binder;a hydrocarbon feed inlet constructed and arranged to ...

PRODUCTION OF DIESEL AND BASE STOCKS FROM CRUDE OIL

A process of producing Group III base oils, along with a naphtha product and diesel product, from whole waxy crude oil is provided. The inventive process omits the typical vacuum distillation stage and separations to form the typical cuts off of the vacuum tower. By selecting a waxy crude oil suitable for processing without separations, the crude oil may be hydroprocessed, dearomatized, dewaxed, and hydrofinished to produce a Group III base oil. Additionally, the dewaxing catalyst will isomerize the naphtha range molecules to increase the octane value to a suitable level for blending into gasoline and the diesel range molecules to reduce the diesel cloud point. 1. A method for producing lubricant base oils from a whole petroleum crude oil , comprising:a. providing a whole petroleum crude oil feedstock comprising less than about 2 wt % of heptane asphaltenes, less than about 2 wt % of Conradson carbon residue (CCR), and less than about 50 ppm of metals;b. hydrotreating the whole petroleum crude oil feedstock on at least one bed of a hydrotreating catalyst under effective hydrotreating conditions to produce a hydrotreated effluent having less sulfur, nitrogen and aromatics than the whole petroleum crude oil;c. dewaxing the hydrotreated effluent in the presence of a dewaxing catalyst to produce a naphtha product having an octane value greater than 60, a diesel product having a cloud point less than 0° C., and a lubricant base oil product; andd. fractionating the lubricant base oil product into at least a low viscosity lubricant base oil product having a viscosity of 2-8 cSt at 100° C. and a high viscosity lubricant base oil product having a viscosity of 6-30 cSt at 100° C.2. The method of claim 1 , wherein the low viscosity lubricant base oil product and the high viscosity lubricant base oil product have a viscosity index of at least 120 claim 1 , a pour point of about −15° C. claim 1 , and less than 300 ppm sulfur.3. The method of claim 1 , wherein the naphtha product ...

CATALYST WITH IMPROVED ACTIVITY/SELECTIVITY FOR LIGHT NAPHTHA AROMATIZATION

In an aspect, a method for the aromatization of hydrocarbons comprises contacting a hydrocarbon feedstream with a catalyst; wherein the catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the zeolite further comprises Na; and wherein the catalyst has an Si:Almole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5, wherein the catalyst has an aluminum content of less than or equal to 0.75 wt % excluding any binder and extrusion aide. 1. A method for the aromatization of hydrocarbons comprising:contacting a hydrocarbon feedstream with a catalyst;wherein the catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the zeolite further comprises Na; and{'sub': '2', 'wherein the catalyst has an Si:Almole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5, wherein the catalyst has an aluminum content of less than or equal to 0.75 wt % excluding any binder and extrusion aide.'}2. The method of claim 1 , wherein the hydrocarbon feedstream comprises an olefinic compound.3. The method of claim 1 , wherein the hydrocarbon feedstream comprises an alkane compound.4. The method of claim 3 , wherein the alkane compound comprises a Calkane.5. The method of claim 3 , wherein the alkane compound comprises a Calkane.6. The method of claim 5 , wherein the feed stream comprises 20 to 100 vol % of at least one of the C claim 5 , C claim 5 , or Calkane.7. The method of claim 1 , wherein the hydrocarbon feedstream comprises naphthene.8. The method of claim 1 , wherein the hydrocarbon feedstream comprises a naphtha feed.9. The method of claim 8 , wherein the naphtha feed comprises up to 1 claim 8 ,000 parts per million by weight sulfur and/or up to 100 parts per million by weight of nitrogen compounds.10. The method of claim 1 , wherein the Ge is present in an amount of ...

METHOD AND SYSTEM FOR PRODUCING AROMATIC HYDROCARBONS FROM A RENEWABLE RESOURCE

Disclosed are a method and a system for producing bio-derived aromatic hydrocarbons from a renewable resource. More particularly, the disclosure provides for the co-location of a biomass reactor unit and an aromatization reactor unit to produce benzene from a renewable source such as plant mass. Hexane produced from cellulose in the biomass reactor unit can be converted to benzene in the aromatization reactor unit and hydrogen produced in the aromatization reactor unit can be used in the biomass reactor unit. Also described is the use of a mixture of bio-derived hexane produced from cellulose and naphtha in an aromatization process. 1. A method for producing a bio-derived aromatic hydrocarbon , comprising:a) contacting a biomass with hydrogen in the presence of a hydrodeoxygenation catalyst in at least one hydrodeoxygenation reactor unit, under conditions that produce a bio-derived feedstock further comprising paraffinic, naphthenic, and/or olefinic hydrocarbons;b) introducing the bio-derived feedstock into at least one aromatization reactor unit and contacting the bio-derived feedstock with an aromatization catalyst under conditions that produce an aromatic hydrocarbon and hydrogen; andc) providing at least a portion of the hydrogen produced in the at least one aromatization reactor to the at least one hydrodeoxygenation reactor for contacting the biomass.2. The method of claim 1 , wherein the hydrodeoxygenation reactor unit is located proximate to the at least one aromatization reactor unit.3. The method of claim 1 , wherein the bio-derived feedstock comprises C6 to C8 paraffinic claim 1 , naphthenic claim 1 , and olefinic hydrocarbons.4. The method of claim 1 , wherein the bio-derived feedstock comprises a hexane.5. The method of claim 1 , wherein the aromatic hydrocarbon comprises one or more of benzene claim 1 , toluene claim 1 , or xylenes.6. The method of claim 1 , wherein the biomass comprises a cellulose claim 1 , a sugar claim 1 , a starch claim 1 , a ...

Method and system for producing aromatic hydrocarbons from a renewable resource

Disclosed are a method and a system for producing bio-derived aromatic hydrocarbons from a renewable resource. More particularly, the disclosure provides for the co-location of a biomass reactor unit and an aromatization reactor unit to produce benzene from a renewable source such as plant mass. Hexane produced from cellulose in the biomass reactor unit can be converted to benzene in the aromatization reactor unit and hydrogen produced in the aromatization reactor unit can be used in the biomass reactor unit. Also described is the use of a mixture of bio-derived hexane produced from cellulose and naphtha in an aromatization process.

Hydroprocessing scheme for production of premium isomerized light gasoline

A hydroconversion catalyst composition includes a catalytically active matrix having a surface area of between about 50 m 2 /g to about 290 m 2 /g, a silicious molecular sieve support medium distributed through the matrix and having a surface area of between about 250 m 2 /g to about 1200 m 2 /g and a catalytically active phase supported on the support medium and including a first metal selected from group IIIA of the periodic table of elements and a second metal selected from group VIB of the periodic table of elements. The matrix preferably further includes aluminum, gallium, cobalt, molybdenum, and phosphorus.

Process for producing reformulated gasoline by reducing sulfur, nitrogen and olefin

A process for upgrading a nitrogen and sulfur rich heavy naphtha feedstock includes the steps of providing a naphtha feedstock having an initial nitrogen content, an initial sulfur content and an initial octane number; contacting the naphtha feedstock with an acid source so as to provide a reduced nitrogen feedstock having a reduced nitrogen content which is less than the initial nitrogen content; contacting the reduced nitrogen feedstock with a hydroconversion catalyst system under a hydrogen atmosphere, temperature and pressure so as to provide a final product having a final nitrogen content which is less than the initial nitrogen content, a final sulfur content which is less than the initial sulfur content, and having a final octane number which is substantially equal to or greater than the initial octane number of the feedstock, and wherein the final product has an increased isomerized component and substantially no increase in aromatic content with respect to the feedstock.

一种费托合成石脑油转化催化剂及其制备方法

一种费托合成石脑油转化催化剂，包括载体和以载体为基准计算的含量如下的活性组分：VA族元素氧化物0.5～15.0质量％，氧化镍0.5～10.0质量％，稀土元素氧化物0.1～3.0质量％，所述的载体包括10～60质量％的ZSM‑5沸石、10～60质量％的Beta沸石和5～40质量％的氧化铝。该催化剂可将费托合成石脑油在非临氢状态下转化为高辛烷值汽油组分和优质液化气，单程反应周期长，再生性能好。

A hydroconversion catalyst

A hydroconversion catalyst composition includes a catalytically active matrix having a surface area of between about 50 m<SP>2</SP>/g to about 290 m<SP>2</SP>/g, a silicious molecular sieve support medium distributed through the matrix and having a surface area of between about 250 m<SP>2</SP>/g to about 1200 m<SP>2</SP>/g and a catalytically active phase supported on the support medium and including a first metal selected from group IIIA of the periodic table of elements eg. Ga or B, a second metal selected from group VIB of the periodic table of element eg. Cr or Mo. The matrix preferably further includes aluminum, gallium, cobalt, molybdenum, and phosphorus.

Hydrocarbon conversion catalysts

脱水素環化法

(57)【要約】本公報は電子出願前の出願データであるた め要約のデータは記録されません。

Crystalline zeolite zsm-5 and method of preparing the same

A FAMILY OF CRYSTALLINE ZEOLITES, DESIGNATED ZSM-5, HAVING THE COMPOSITION, EXPRESSED AS MOLE RATIOS OF OXIDES AS FOLLOWS: 0.9$0.2M2/NO:W2O3:5-100YO2:ZH2O WHEREIN M IS AT LEAST ONE CATION, N IS THE VALENCE THEREOF, W IS SELECTED FROM THE GROUP CONSISTING OF ALUMINUM AND GALLIUM, Y IS SELECTED FROM THE GROUP CONSISTING OF SILICON AND GERMANIUM, AND Z IS FROM 0-40, AND CHARACTERIZED BY A SPECIFIED X-RAY POWDER DIFFRACTION PATTERN. CATALYTIC CONVERSION CARRIED OUT IN THE PRESENCE OF SUCH ZEOLITES.

Methods of regenerating aromatization catalysts

Methods for treating or rejuvenating a spent catalyst are described. These methods can employ a step of halogenating the spent catalyst, followed by decoking the halogenated spent catalyst. The halogenation step can utilize fluorine and chlorine together, or fluorine and chlorine can be applied sequentially.

Aromatization catalysts with high surface area and pore volume

Regenerable aromatization catalysts having high surface area and pore volume, as well as methods for producing these catalysts, are disclosed.

Process for regenerating sulfur contaminated reforming catalysts

The present invention is a process for regenerating a sulfur-contaminated, highly selective, large-pore zeolite catalyst. It comprises a multistep process involving exposure of the catalyst to a combination of oxidizing conditions, reducing conditions and treatment with a halogen acid gas. These conditions are effective to agglomerate a Group VIII metal and remove sulfur. Thereafter, the catalyst is oxychlorinated to redisperse the Group VIII metal over the catalyst surface. A carbon removal step is optionally included.

Regeneration of a platinum-containing zeolite

A method is described for the regeneration of a hydrocarbon conversion catalyst that has become deactivated by carbonaceous material deposition where the catalyst comprises a nonacid zeolite and a Group VIII metal component. The method comprises the steps of (1) removing a substantial portion of the carbonaceous material from the catalyst by combustion with an oxygen-containing gas in the presence of a halogen, and (2) reducing the catalyst in the presence of hydrogen.

Upgradation of undesirable olefinic liquid hydrocarbon streams

A process for converting undesirable olefinic hydrocarbon streams to hydrogen and petrochemical feedstock e.g. light olefins in C 2 -C 4 range and aromatics especially toluene and xylenes, which comprises simultaneous cracking and reforming at olefin rich hydrocarbons using a catalyst consisting of dehydrogenating metal components, shape selective zeolite components and large pore acidic components in different proportions in a circulating fluidized bed reactor-regenerator system having reactor temperature within 450-750° C. and WHSV of 0.1-60 hour -1 .

Fractionating and further cracking a C6 fraction from a naphtha feed for propylene generation

The present invention relates to a process for selectively producing C 3 olefins from a catalytically cracked or thermally cracked naphtha stream by fractionating the naphtha feed to obtain a C 6 fraction and feeding the C 6 fraction either in the riser downstream of the injection point for the reminder of the naphtha feed, in the stripper, and/or in the dilute phase immediately downstream or above the stripper of a process unit.

Hydrocarbon conversion process using a zeolite bound zeolite catalyst

Zeolite catalyst and process for using said catalyst

Iron, cobalt and/or nickel containing ALPO bound SAPO molecular sieve catalyst for producing olefins

An aluminophosphate bound silicoaluminophosphate catalyst contains iron, cobalt and/or nickel is useful in a method of making a product including an olefin from a feedstock containing an oxygenate. The method includes contacting an oxygenate feedstock with the catalyst, which is an aluminophosphate bound silicoaluminophosphate catalyst containing iron, cobalt and/or nickel and which does not contain a significant amount of amorphous binder, in its activated state under conditions effective to produce an olefin product.

Conversion of hydrocarbons with a catalyst comprising a halogen component combined with a support containing alumina and finely divided crystalline aluminosilicate particles

HYDROCARBONS ARE CONVERTED WITH A CATALYST COMPRISING A HALOGEN COMPONENT COMBINED WITH A SUPPORT CONTAINING ALUMINA AND FINELY DIVIDED CRYSTALLINE ALUMINOSILICATE PARTICLES. KEY FEATURE OF THE PROCESS INVOLVES THE PREPARATION OF THE CATALYST FROM AN ALUMINUM HYDROXYL HALIDE SOL TO WHICH FINELY DIVIDED PARTICLES OF CRYSTALLINE ALUMINOSILICATE ARE ADDED, THEREBY EFFECTING SOME BASIC ENHANCEMENT OF THE ABILITY OF THE RESULTANT CATALYST TO ACCELERATE HYDROCARBON CONVERSION REACTIONS THAT DEPEND ON CARBONIUM ION INTERMEDIATES: THAT IS, THE ACIDITY LEVEL OF THE RESULTANT COMPOSITE IS MARKEDLY INCREASED. IN ADDDITION, THIS CATALYST CAN BE COMBINED WITH A GROUP VI OR GROUP VIII METALLIC COMPONENT AND UTILIZED IN A PROCESS DESIGNED TO ACCELERATE A WIDE VARIETY OF REACTIONS OF THE TYPE WHICH HAVE HERETOFORE UTILIZED DUAL-FUNCTION CATALYSTS SUCH AS HYDRO-CRACKING, REFORMING, ISOMERIZATION, ETC.

Conversion of light naphtha to enhanced value products in an integrated two-zone reactor process

An integrated process for conversion of a hydrocarbon stream comprising light naphtha to enhanced value products. The process includes passing the hydrocarbon stream through a first reactor, the first reactor being a catalytic bed reactor with a dual-function catalyst to simultaneously reform light naphtha to BTEX and crack light naphtha to ethane, propane, and butanes. Further, the process includes passing an effluent of the first reactor to a gas-liquid separating unit to generate a liquid stream and a gas stream, and passing the gas stream to a gas separator unit to remove hydrogen gas and methane and generate an enhanced gas stream. The process further includes passing the enhanced gas stream through a second reactor, the second reactor being a pyrolysis unit operated at steam cracking conditions to convert ethane, propane, and butanes in the enhanced gas stream to light. An associated system for performing the process is also provided wherein the integrated process does not include passage of a process stream to a separate and independent hydrocracking unit to crack light alkanes in the hydrocarbon stream to smaller alkanes.

Katalysator for hyte fo r fremstilling av aromatiske hydrokarboner.

Katalysator for hyte fo r fremstilling av aromatiske hydrokarboner.

Manufacturing a base stock from ethanol

A systems and method for manufacturing a base stock from an ethanol stream are described herein. An example method includes dehydrating an ethanol stream to form an impure ethylene mixture, recovering an ethylene stream from the impure ethylene mixture, and oligomerizing the ethylene stream to form a raw oligomer stream. A heavy olefinic stream is distilled from the raw oligomer stream. The heavy olefinic stream is hydro-processed to form a hydro-processed stream, and the hydro-processed stream is distilled to form the base stock.

METHOD FOR PRODUCING A CATALYST.

Zeolite-l catalyst and process for using said catalyst

Method for increasing yield of liquid hydrocarbon product

FIELD: gasoline production. SUBSTANCE: invention relates to a method for increasing the yield of a liquid hydrocarbon product and/or the selective formation of С 5+ hydrocarbons in a method for producing gasoline, in which three streams are used as raw material, the first of which comprises a hydrocarbon fraction representing gasoline fraction with an end-boiling point of no more than 215°C, a second stream includes oxygenate, which is at least one component selected from the group: methanol, ethanol, dimethyl ether, the third stream includes the olefin-containing fraction. The olefin-containing fraction comprises one or more olefins selected from a group comprising ethylene, propylene, normal butylene, isobutylene, in a total quantity of 10 to 50 wt.%. In this method, three reaction zones are used, filled with a zeolite catalyst, which comprises a zeolite of type ZSM-5. The first flow is fed into at least one reaction zone, the second flow is distributed into three reaction zones, the third flow is distributed into three reaction zones. The product flow from the first reaction zone is fed into the second reaction zone, and the product flow from the second reaction zone is fed into the third reaction zone, wherein the temperature at the input of each subsequent reaction zone is higher than the temperature at the input of each previous zone. The hydrocarbon fraction is 62-88 wt.% of the feedstock and the olefin-containing fraction is 7-33 wt.% of the feedstock. The flow temperature at the inlet to the first / second / third reaction zone is 330-350°C / 340-360°C / 350-370°C. The distribution of the second flow between the three reaction zones is 40-60 wt.% / 20-40 wt.% / 10-30 wt. %, the distribution of the third flux between the three reaction zones is 20-40 wt.% / 25-45 wt. % / 25-45 wt.%, catalyst distribution by reaction zones is 10-30 wt.% / 20-40 wt.% / 40-60 wt.% of the total catalyst for the first / second / third reaction zone respectively. EFFECT: technical ...

Method for production of n-alkanes from mineral oil fractions and catalyst for carrying out said method

The invention relates to a method for the production of n-alkanes from mineral oil fractions and fractions from thermal or catalytic conversion plants, containing cyclic alkanes, alkenes, cyclic alkenes and/or aromatics. The invention further relates to a catalyst for carrying out said method.

Stable, high-yield reforming catalyst

A reforming process, selective for the dehydrocyclization of paraffins to aromatics, is effected using a bed of catalyst particles containing multiple Group VIII (8-10) noble metals having different gradients within the catalyst particles and a nonacidic large-pore molecular sieve. The use of this bed of catalyst particles results in greater selectivity of conversion of paraffins to aromatics and improved catalyst stability, particularly in the presence of small amounts of sulfur.

Stable, high-yield reforming catalyst

A reforming process, selective for the dehydrocyclization of paraffins to aromatics, is effected using a bed of catalyst particles containing multiple Group VIII (8-10) noble metals having different gradients within the catalyst particles and a nonacidic large-pore molecular sieve. The use of this bed of catalyst particles results in greater selectivity of conversion of paraffins to aromatics and improved catalyst stability, particularly in the presence of small amounts of sulfur.

Catalytic system for low-temperature reforming of gasoline factions and method for its implementation with use of catalytic system

FIELD: technological processes.SUBSTANCE: invention relates to a catalyst system for a low temperature reforming process for gasoline fractions comprising three reactors connected in series with granular catalysts, the first of which comprises a catalyst having a composition, by weight: platinum 0.1–0.3, AEL structure zeolite 10.0–60.0, the rest being alumina, and the second and third reactors contain catalyst composition, wt. %: platinum 0.1–0.3, magnesium 1.8–2.1, LTL structure zeolite 10.0–60.0, the rest being alumina, the ratio of the volume of catalysts in the reactors, respectively, is: 1:1–2:1–4. Also, the invention relates to a process for reforming gasoline fractions using the claimed catalytic system.EFFECT: technical result consists in increasing the yield of the desired product and improving its composition at a lower process temperature.2 cl, 1 dwg, 5 tbl, 7 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 670 108 C1 (51) МПК B01J 29/068 (2006.01) B01J 29/62 (2006.01) B01J 29/22 (2006.01) B01J 29/44 (2006.01) B01J 29/85 (2006.01) C10G 35/095 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 29/068 (2006.01); B01J 29/62 (2006.01); B01J 29/22 (2006.01); B01J 29/44 (2006.01); B01J 29/85 (2006.01); C10G 35/095 (2006.01) (21)(22) Заявка: 2017121532, 20.06.2017 20.06.2017 Дата регистрации: 18.10.2018 (45) Опубликовано: 18.10.2018 Бюл. № 29 Адрес для переписки: 117997, Москва, Софийская наб., 26/1, ПАО "НК "Роснефть", ДНТРиИ, Антимоновой Е.П. 2 6 7 0 1 0 8 C 1 (56) Список документов, цитированных в отчете о поиске: US 6740228 B1, 25.05.2004. US 20150165422 A1, 18.06.2015. US 8349754 B2, 08.01.2013. WO 2017019958 A1, 02.02.2017. RU 2574404 C2, 10.02.2016. (54) Каталитическая система для низкотемпературного риформинга бензиновых фракций и способ его осуществления с применением каталитической системы (57) Реферат: Изобретение относится к каталитической остальное, причем отношение объема системе для ...

UZM-45 aluminosilicate zeolite, method of preparation and processes using UZM-45

A new family of crystalline aluminosilicate zeolites has been synthesized designated UZM-45. These zeolites are represented by the empirical formula. M m n+ R r p+ Al (1-x) E x Si y O z where M is an alkali, alkaline earth, or rare earth metal such as lithium and strontium, R is an organoammonium cation such as the choline cation and E is a framework element such as gallium. These zeolites are characterized by unique x-ray diffraction patterns and compositions and have catalytic properties for carrying out various hydrocarbon conversion processes.

Metallophosphate molecular sieves, methods of preparation and use

A new family of crystalline microporous metallophosphates designated AlPO-59 has been synthesized. These metallophosphates are represented by the empirical formula R + r M m 2+ EP x Si y O z where R is an organoammonium cation such as the ETMA + , M is a framework metal alkaline earth or transition metal of valence 2+, and E is a trivalent framework element such as aluminum or gallium. The AlPO-59 compositions are characterized by a new unique ABC-6 net structure and compositions and have catalytic properties for carrying out various hydrocarbon conversion processes, and separation properties for separating at least one component.

High charge density silicometallophosphate molecular sieves SAPO-79

A new family of high charge density crystalline microporous silicometallophosphate designated SAPO-79 has been synthesized. These silicometallophosphate are represented by the empirical formula of: R p+ r M m + E x PSi y O z where M is an alkali metal such as potassium, R is an organoammonium cation such as diethyldimethylammonium and E is a trivalent framework element such as aluminum or gallium. The SAPO-79 family of materials represent the first alkali-stabilized phosphate-based molecular sieves to have the ERI topology and have catalytic properties for carrying out various hydrocarbon conversion processes and separation properties for separating at least one component.

用于石脑油催化重整的抗硫中毒核-壳催化剂的制备方法

本发明属于石油化工技术领域，具体涉及一种用于石脑油催化重整的抗硫中毒核‑壳催化剂的制备方法，筛网筛分γ‑Al 2 O 3 ，清洗后干燥并焙烧；取γ‑Al 2 O 3 放入氨水中进行活化，并干燥；将γ‑Al 2 O 3 在氯铂酸钾溶液浸泡，并干燥和焙烧；配制ZSM‑5分子筛合成液，采用去离子水为溶质，正硅酸乙酯为硅源，四丙基氢氧化铵为模板剂，异丙醇铝为铝源，配制成均匀稳定的乳浊液型成膜液；将Pt/Al 2 O 3 和ZSM‑5制备Pt/Al 2 O 3 ‑ZSM‑5；将Pt/Al 2 O 3 ‑ZSM‑5在氢氧化钾水溶液中浸泡；将Pt/Al 2 O 3 ‑ZSM‑5放入去离子水中浸泡，烘干并焙烧。该催化剂对硫化物实现抗中毒效果。

The method of production increase of benzene from hydrocarbon feedstock

A method for production increase of benzene from hydrocarbon mixture is provided to combine the process of manufacturing aromatic hydrocarbon mixture and LPG from hydrocarbon mixture and the solvent extracting process for separating polar hydrocarbon from hydrocarbon mixture. The method for production increase of benzene from hydrocarbon mixture including the steps of: (a) separating hydrocarbon mixture into hydrocarbon flow of less than C6 and hydrocarbon flow of more than C7; (b) separating non-aromatic hydrocarbon flow and aromatic carbon flow from hydrocarbon of less than C6 through solvent extracting process; (c) collecting benzene from aromatic hydrocarbon flow; (d) flowing hydrocarbon of more than C7 and hydrogen into on reaction area; (e) converting hydrocarbon of more than C7 to aromatic hydrocarbon by dealkylation or transalkylation and then converting it to non-aromatic hydrocarbon by hydrocracking; (f) separating the reaction product of step(e) into upper flow and a bottom flow; and (g) collecting benzene, toluene, xylene and aromatic compound of more than C9 from the bottom flow.

用于调节介孔核-壳催化剂壳层疏水性的表面修饰方法

本发明属于石油化工技术领域，具体涉及一种用于调节介孔核‑壳催化剂壳层疏水性的表面修饰方法，1、核壳催化剂的可调节疏水改性；将核壳催化剂氨水溶液中浸渍后烘干；将上述核壳催化剂放入氨丙基三乙氧基硅烷乙醇溶液一段时间后倒出溶液，取出并控干液体；将上述催化剂放置在离子水液面上方聚四氟乙烯孔板支架，密封并放置于烘箱内合成；将上述催化剂固体用去离子水冲洗后用无水乙醇浸泡或冲洗，并烘干，再将其置于马弗炉中焙烧；2、通过调节氨丙基三乙氧基硅烷乙醇溶液的浓度，来改变其在介孔MSU‑1孔道及外表面的丰度和分布，通过提高其的含量提高MSU‑1壳层的疏水性。疏水性调节能够明显提高核壳结构的抗中毒性。

Method of regenerating flavouring catalyst using decoking step between steps of adding chlorine and fluorine

FIELD: chemistry. SUBSTANCE: invention relates to methods of spent catalyst regeneration. Described is a method of recovering a spent catalyst containing a transition metal of group 8–11 and a catalyst support, involving: (1) contacting the catalyst with a chlorine-containing stream containing a chlorine-containing compound in a gas phase to obtain a chlorinated spent catalyst; (2) contacting chlorinated spent catalyst with a coke burning gas stream containing oxygen to obtain a decanted catalyst; (3) contacting the decanted catalyst with a fluorine-containing solution containing a fluorine-containing compound in a liquid phase to obtain a fluorinated catalyst; and the catalyst support includes a zeolite with large pores, having average pore diameter of about 7 to about 12 Å. EFFECT: technical result is improved methods of reducing catalytic activity of spent catalysts. 41 cl, 3 ex, 2 tbl, 8 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК B01J 38/42 B01J 32/00 B01J 38/12 B01J 38/46 B01J 38/48 B01J 29/90 ФЕДЕРАЛЬНАЯ СЛУЖБА B01J 29/62 ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ C10G 35/06 (12) (11) (13) 2 738 157 C1 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 38/42 (2020.08); B01J 32/00 (2020.08); B01J 38/12 (2020.08); B01J 38/46 (2020.08); B01J 38/48 (2020.08); B01J 29/90 (2020.08); B01J 29/62 (2020.08); C10G 35/06 (2020.08) (21)(22) Заявка: 2019136624, 17.05.2018 17.05.2018 08.12.2020 Приоритет(ы): (30) Конвенционный приоритет: (56) Список документов, цитированных в отчете о поиске: US 2013/0231512 A1, 05.09.2013. US 2004/0259719 A1, 23.12.2004. RU 2014134746 A, 27.04.2016. US 20140213839 A1, 31.07.2014. US 9421529 B2, 23.08.2016. US 3418256 A, 24.12.1968. RU 2500476 C2, 10.12.2013. 17.05.2017 US 15/597,184 (45) Опубликовано: 08.12.2020 Бюл. № 34 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 17.12.2019 2 7 3 8 1 5 7 (73) Патентообладатель(и): ШЕВРОН ФИЛЛИПС КЕМИКАЛ КОМПАНИ ЭлПи (US) ...

应用沸石结合沸石催化剂的烃转化过程

公开了一种利用沸石结合沸石催化剂转化烃类的一个过程,这种催化剂在烃转化过程的应用中已经提高了性能,如在催化裂化,甲苯歧化,异构化作用,及烷基转移反应中,这种催化剂由第一沸石,及第二沸石组成第一沸石具有大于0.1微米的平均粒径,第二沸石的平均粒径比第一沸石小。

Single step catalytic process for conversion of n-paraffins and naphtha to diesel-range hydrocarbons

FIELD: chemistry. SUBSTANCE: present invention relates to a one-stage catalytic process for the conversion of n-paraffins and naphtha to diesel-range hydrocarbons (diesel fuel). Described is a single-step catalytic method for the conversion of n-paraffins and naphtha (90-140°C) to diesel-range hydrocarbons using a solid acid catalyst Pt-Sn-ZSM-5, in which said method comprises loading a Pt-Sn-ZSM-5 catalyst into a reactor, reduction of the catalyst with hydrogen at a temperature from 500 to 600°C for 6 to 10 hours by flowing hydrogen gas at 6-16 l / h, with subsequent introduction of a continuous feed stream with a weight hourly space velocity (WHSV) of 2 to 10 h -1 at a temperature in the range from 400 to 450°C with a carrier gas at a volumetric flow rate from 5 to 50 l / h and a reactor pressure from 2 to 30 bar, to obtain liquid products and gas products, in which the liquid products are diesel-range hydrocarbons and gasoline, where in the Pt-Sn-ZSM-5 catalyst, the percentage content of Pt and Sn is in the range of 0.1 to 1.0 wt% and 0.2 to 1.6 wt%, respectively. EFFECT: technical result is a bimetallic catalyst Pt-Sn-ZSM-5 for direct conversion of n-heptane, as well as naphtha, to diesel-range hydrocarbons in a single-step process. 17 cl, 3 tbl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 648 239 C2 (51) МПК C10G 35/09 (2006.01) C10G 35/095 (2006.01) B01J 23/62 (2006.01) B01J 29/44 (2006.01) B01J 37/02 (2006.01) B01J 37/18 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 35/09 (2006.01); C10G 35/095 (2006.01); B01J 29/44 (2006.01); B01J 37/02 (2006.01); B01J 37/18 (2006.01); B01J 23/62 (2006.01); B01J 29/40 (2006.01); B01J 37/00 (2006.01); B01J 37/16 (2006.01) (21)(22) Заявка: 2015121912, 11.11.2013 11.11.2013 Дата регистрации: 23.03.2018 09.11.2012 IN 3485/DEL/2012 (43) Дата публикации заявки: 27.12.2016 Бюл. № 36 (56) Список документов, цитированных в отчете о поиске: RU 2357799 C2, 10.06.2009 ...

Method of making an improved catalyst containing an acid-treated zeolite, a boron component, and a zinc component, a product from such method, and the use thereof in the conversion of hydrocarbons

An improved zeolite catalyst containing an acid-treated zeolite, a boron component and a zinc component manufactured by a novel method having certain process steps necessary for providing the improved zeolite catalyst. The process steps include a first steam treatment of an acid-treated zeolite, followed by incorporation of such zeolite with a boron component and a zinc component, followed by a second steam treatment. Processes are also disclosed for using the improved zeolite catalyst in the conversion of hydrocarbons, preferably non-aromatic hydrocarbons, to lower olefins (such as ethylene and propylene) and aromatic hydrocarbons (such as benzene, toluene, and xylene).

Fractionating and further cracking a c6 fraction from a naphtha feed for propylene generation

본 발명은 나프타-비등-범위 공급물 스트림 및/또는 생성물 스트림으로부터 분리된 C 6 -풍부 분획을 공급물로부터 다운스트림에서 분해 단계로 주입함으로써, 접촉 분해되거나 열분해된 나프타 스트림으로부터 C 3 올레핀을 선택적으로 생성시키는 방법에 관한 것이다. The present invention provides for selective C 3 olefins from catalytically cracked or pyrolyzed naphtha streams by injecting a C 6 -rich fraction separated from the naphtha-boiling-range feed stream and / or product stream into the cracking stage downstream from the feed. It relates to a method of generating.

Method for producing gasoline with distribution of oxygenate and two olefin-containing fractions

FIELD: gasoline production. SUBSTANCE: invention relates to a method for producing gasoline, in which four streams are used as raw material, the first of which comprises a hydrocarbon fraction which is in the form of a gasoline fraction having a boiling point of not more than 215°C, and the second stream comprises an oxygenate, at least one component selected from the group: methanol, ethanol, dimethyl ether, third flow includes the first olefin-containing fraction, fourth flow includes the second olefin-containing fraction. The first olefin-containing fraction comprises one or more olefins selected from a group comprising ethylene, propylene, butylene, isobutylene, in a total quantity of 10 to 50 wt.% and includes 0.5-8.0 wt.% hydrogen. The second olefin-containing fraction comprises one or more olefins selected from the group comprising propylene, butylene and isobutylene in a total quantity of 50 to 70 wt.% and includes 0 to 5.0 wt.% of C1-C2 hydrocarbons. The inventive method consists in using three reaction zones filled with a zeolite catalyst which comprises ZSM-5-type zeolite. The first flow is fed into at least one reaction zone, the second flow is fed into the first, second and third reaction zones, wherein the mass fraction of the second flow delivered to each subsequent reaction zone is less than the mass fraction of the second flow, the third stream is fed into at least one reaction zone and the fourth stream is fed into at least one reaction zone. The product flow from the first reaction zone is fed into the second reaction zone and the product flow from the second reaction zone is fed into the third reaction zone. The hydrocarbon fraction is 70-83 wt.% of the feedstock, the first olefin-containing fraction is 4-19 wt.% of the feedstock, the second olefin-containing fraction is 3-14 wt.% of the feedstock. The distribution of the second flow between the three reaction zones is 40-85 wt.%/10-35 wt.%/5-25 wt.% of the total amount of the second flow and the ...

Method of synthesis of aromatic hydrocarbons (variants)

FIELD: organic chemistry, chemical technology, petroleum chemistry. SUBSTANCE: method of synthesis of aromatic hydrocarbons involves the conversion of a mixture of methane with at least one C 2 -C 12 -hydrocarbon in the volume ratio methane/hydrocarbon raw = 500, not above, at temperature 300-1000 C, under pressure 10 MPa, not above, in volume consumptions of hydrocarbon mixture 10000 h -1 , not above, in the presence of the porous catalyst. As a catalyst the following substances can be used: either zeolite of alumosilicate composition taken among the order: ZSM-5, ZSM-11, ZSM-35, ZSM-38, ZSM-48, BETA that has a mole ratio SiO 2 /Al 2 O 3 = 450, not above, or gallosilicate, galloalumosilicate, iron silicate, iron-alumosilicate, chrome silicate, chrome-alumosilicate of the structure ZSM-5, ZSM-11, ZSM-48, BETA or alumophosphate of the structure of type ALPO-5, ALPO-11, ALPO-31, ALPO-36, ALPO-37, ALPO-40 with elements incorporated in the structure on the stage of synthesis and taken among the order: magnesium, zinc, gallium, manganese, iron, silicon, cobalt, cadmium. Catalyst for all variant of the method can comprise additionally zinc, and/or gallium, and/or rare-earth elements, or metal of the platinum group taken in the amount 10 wt.%, not above. EFFECT: improved method of synthesis, enhanced yield of aromatic hydrocarbon. 15 cl, 23 ex сс с ПЧ Го РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) (51) МПК? ВИ” 2188 225. 13) СЛ С 10 С 35/095, С 07 С 15/00 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 2001104362/04, 19.02.2001 (24) Дата начала действия патента: 19.02.2001 (46) Дата публикации: 27.08.2002 (56) Ссылки: Ц$ 4891463 А, 02.01.1990. КЦ 2135441 СЛ, 27.08.1999. 4$ 5998686 А, 07.12.1999. 4$ 4629818 А, 16.12.1986. КЦ 2138538 СЛ, 27.09.1999. КЦ 2092240 СЛ, 10.10.1997. (98) Адрес для переписки: 630090, г.Новосибирск, пр. Академика Лаврентьева, $, Институт катализа им. Г.К. Борескова, патентный отдел, Т.Д.Юдиной (71) Заявитель: ...

Process for The Preparation of Aromatic Hydrocarbons and Liquefied Petroleum Gas from Hydrocarbon Mixture

본 발명은 탄화수소 혼합물로부터 방향족 탄화수소 및 액화석유가스를 제조하는 공정에 관한 것으로, 제올라이트와 무기질 바인더로 이루어진 혼합담체에 백금/비스무트를 담지시켜 된 촉매의 존재 하에서 탄화수소 원료 혼합물 중 비방향족 화합물은 수소첨가분해 반응을 통하여 액화석유가스(LPG)가 풍부한 기상물질로 전환되고, 방향족 화합물은 탈알킬화 및 트랜스알킬화 반응을 통하여 벤젠, 톨루엔, 자일렌 등이 풍부한 유분으로 전환된다. 상기 기상생성물은 증류과정을 통해서 비점 차이를 이용하여 LPG 및 메탄과 에탄의 혼합물로 분리되며, 액상생성물은 증류과정을 통해서 비점 차이에 의하여 벤젠, 톨루엔, 자일렌, C9+ 방향족 화합물 등으로 분리되어 각각 수득된다. 탄화수소, 액화석유가스, 제올라이트, 백금, 비스무트, 수소첨가 분해, 탈알킬화, 트랜스알킬화 The present invention relates to a process for producing an aromatic hydrocarbon and liquefied petroleum gas from a hydrocarbon mixture, wherein the non-aromatic compound in the hydrocarbon raw material mixture is hydrogenated in the presence of a catalyst having platinum / bismuth supported on a mixed carrier composed of zeolite and an inorganic binder. The decomposition reaction converts LPG into a gaseous substance rich in liquefied petroleum gas (LPG), and the aromatic compound is converted into an oil rich in benzene, toluene and xylene through dealkylation and transalkylation. The gaseous product is separated into a mixture of LPG and methane and ethane using a boiling point difference through a distillation process, and the liquid product is separated into a benzene, toluene, xylene, C9 + aromatic compound and the like by a boiling point difference through a distillation process, respectively. Obtained. Hydrocarbon, liquefied petroleum gas, zeolite, platinum, bismuth, hydrocracking, dealkylation, transalkylation

Process for selective ring opening of cyclic hydrocarbons

본 발명은 고리형 탄화수소의 고리열림 반응공정 및 그 공정에 사용되는 촉매에 관한 것으로서, 금속성분과 산점을 동시에 함유한 이중기능성 촉매를 이용하여 납센 (고리형 탄화수소)의 선택적 고리열림 반응 (selective ring opening) 수행시 환원제 H 2 만을 단독으로 사용하는 경우와 비교하여 H 2 및 CO 2 를 동시에 사용하거나, CO 2 만을 사용하여도 H 2 만을 사용하는 경우와 같거나 혹은 더 우수한 전환율 및 선택도를 보이는 기술에 관한 것이다. 또한 본 발명에서 고리열림반응에 의한 생성물은 원료물질 보다 세탄가가 개선되어 디젤연료의 질을 증진하는 방법을 제공하는 것이다. The present invention relates to a ring opening reaction process of a cyclic hydrocarbon and a catalyst used in the process, wherein a selective ring opening reaction of leadene (cyclic hydrocarbon) using a bifunctional catalyst containing a metal component and an acid point at the same time When performing the opening, H 2 and CO 2 are used at the same time compared to the case where only the reducing agent H 2 is used alone, or even when CO 2 alone is used, the conversion or selectivity is higher than or equal to that of H 2 alone. It's about technology. In addition, the product of the ring opening reaction in the present invention is to provide a method of improving the quality of diesel fuel by improving the cetane number than the raw material.

Catalyst for gasoline refining

FIELD: oil processing. SUBSTANCE: catalyst has 0.5-5 wt.-% superhighsilicon zeolite type pentasil at the molar ratio SiO 2 /Al 2 O 3 25-90 25-90 and amorphous aluminosilicate basis the rest. Catalyst has additionally also 0.05-2.5 wt.-% zinc oxide or gallium oxide. EFFECT: enhanced quality of catalyst. 2 cl, 1 tbl ЗУЕСУОСсС ПЧ Го РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) (51) МПК ВИ “” 2043 148 ' 13) СЛ В 01 4 29/40, С 10 ©С 35/095 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 93037798/04, 23.07.1993 (46) Дата публикации: 10.09.1995 (56) Ссылки: Левинтер М.Е. и пр. Облагораживание бензинов термического крекинга на ВЫСОКО кремнеземной цеолитсодержащем катализаторе, - Нефтепереработка и нефтехимия, 1991, 3, с.7-9. (71) Заявитель: Мельников В.Б., Макарова Н.П., Вершинин В.И. (72) Изобретатель: Мельников В.Б., Макарова Н.П., Вершинин В.И. (73) Патентообладатель: Мельников Вячеслав Борисович, Гороховский Виктор Анатольевич, Родионов Виктор Иванович (54) КАТАЛИЗАТОР ДЛЯ ОБЛАГОРАЖИВАНИЯ БЕНЗИНОВ (57) Реферат: Использование: нефтепереработка, производство катализаторов для облагораживания бензинов. Сущность изобретения: катализатор содержит 0,5 5 мас. сверхвысококремнеземного цеолита типа пентасил с молярным отношением ЗО 2/А!5О3з 25-90 и аморфную алюмосиликатную основу остальное. Катализатор содержит дополнительно также 0,05 2,5 мас. оксида цинка или оксида галлия. 1 з.п. ф-лы, 1 табл. 2043148 С1 КО ЗУЕСУОСсС ПЧ Го КУЗЗАМ АСЕМСУ ГОК РАТЕМТ$ АМО ТКАОЕМАКК$ 12) АВЗТКАСТ ОЕ 1МУЕМТОМ (19) ВИ “” 2043 148 ' (51) 1пЕ. С1.6 13) Сл В 01 + 29/40, С 10 С 35/095 (21), (22) АррИсаНоп: 9303779804, 23.07.1993 (46) Бае ог ричбИсаНоп: 10.09.1995 (71) АррИсапе: Ме!пкКох М.В., Макагома М.Р., Мегзити \.1. (72) пуетог. — Ме!пКо\ М.В., Макагома М.Р., Мегэитт \М.1. (73) Ргорпеюг: МеГпкох М]аспез!ау Воп$омси, СогокпомзК| Уог Апаю!Гемсп, Кодюпом М!Ког |уапомсИ (54) САТАЕУЗТ РОК САЗОШМЕ ВЕНММС (57) АБзГасЕ: НЕЁСО: о! ргосеззта. ЗОВЗТАМСЕ: саауз{Ё Паз 0.5-5 ...

Uzm-45硅铝酸盐沸石、制备方法和使用uzm-45的方法

已合成了被指定为UZM-45的新的一类结晶硅铝酸盐沸石。所述沸石由下述经验式表示：

Способ регенерации загрязненного серой катализатора ароматизации

Изобретение относится к способу регенерации загрязненного серой катализатора, содержащего переходный металл и подложку катализатора, содержащую цеолит L-типа, включающему промывку загрязненного серой катализатора водным раствором, причем водный раствор, необязательно, содержит щелочной металл, для получения промытого катализатора; приведение в контакт промытого катализатора с раствором галогена, содержащим хлорсодержащее соединение и фторсодержащее соединение, с получением галогенированного катализатора; и прокаливание галогенированного катализатора. Изобретение касается также способа риформинга углеводородного сырья. Технический результат - улучшенное восстановление каталитической активности загрязненных серой катализаторов ароматизации. 2 н. и 58 з.п. ф-лы, 1 табл., 5 пр., 8 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 739 556 C1 (51) МПК B01J 38/54 (2006.01) B01J 38/64 (2006.01) B01J 37/06 (2006.01) B01J 37/24 (2006.01) B01J 37/26 (2006.01) C10G 35/095 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК B01J 38/54 (2020.08); B01J 38/64 (2020.08); B01J 37/06 (2020.08); B01J 37/24 (2020.08); B01J 37/26 (2020.08); C10G 35/095 (2020.08) (21)(22) Заявка: 2019118902, 14.12.2017 14.12.2017 (73) Патентообладатель(и): ШЕВРОН ФИЛЛИПС КЕМИКАЛ КОМПАНИ ЭлПи (US) Дата регистрации: 25.12.2020 20.12.2016 US 15/384,353 (45) Опубликовано: 25.12.2020 Бюл. № 36 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 22.07.2019 (86) Заявка PCT: 2 7 3 9 5 5 6 (56) Список документов, цитированных в отчете о поиске: US 5260238 A1, 09.11.1993. WO 8602861 A1, 22.05.1986. US 6190539 B1, 20.02.2001. US 20100160147 A1, 24.06.2010. US 4987109 A1, 22.01.1991. US 20090156871 A1, 18.06.2009. US 5155074 A1, 13.10.1992. RU 2486008 C2, 27.06.2013. RU 2580553 C2, 10.04.2016. Приоритет(ы): (30) Конвенционный приоритет: R U (24) Дата начала отсчета срока действия патента: (72) Автор(ы): СНЕЛЛ, Райан (US) 2 7 3 9 5 5 6 R U (87) Публикация ...

Компонент катализатора для каталитических превращений углеводородов в нефтехимических процессах

Предложен компонент катализатора для каталитических превращений углеводородов в нефтехимических процессах, представляющий собой синтетический кристаллический алюмосиликат, имеющий химический состав, характеризующийся рентгенограммой.

개질 촉매의 전화를 증가시키는 전처리 방법(pretreatment method for increasing conversion of rxforming catalyst)

촉매를 환원대기하에 1025℉ 내지 1275℉의 온도에서 전처리한 후 수소의 존재하에 탄화수소 공급물과 촉매를 접촉시켜서, 개질 촉매의 전화를 증가시키고 오염율을 저하시키는 전처리 방법이 기재되어 있다.

Комплексная установка для переработки смеси углеводородов с1-с10 различного состава и кислородсодержащих соединений

Настоящее изобретение относится к комплексной установке для переработки смеси углеводородов C-Сразличного состава (низкооктановые бензиновые фракции н.к. - 180°С, 90-160°С или более узкие фракции, пентан-гептановые (гексановые) фракции, пропан-бутановые фракции, ШФЛУ - широкие фракции легких углеводородов - продукт газоперерабатывающих заводов, и/или низшие олефины С-Си/или их смеси друг с другом, и/или с парафинами C-С, и/или с водородом) в присутствии кислородсодержащих соединений, включающей один или более параллельно расположенных секционированных адиабатических реакторов, состоящих из одного и более стационарных слоев (секций) цеолитсодержащего катализатора с подводом или отводом тепла между слоями (секциями) катализатора, или один или более параллельно расположенных изотермических реакторов с тепловыми трубами, и/или змеевиками, и/или трубными теплообменными устройствами, и/или панелями с подводом или отводом тепла с цеолитсодержащим катализатором с возможностью подачи в сырьевую смесь, а также во второй и каждый последующий слой (секцию) с цеолитсодержащим катализатором в адиабатическом реакторе нагретой в огневом или электронагревателе части газа, выделенной в трехфазном сепараторе из потока продуктов реакции после их частичной конденсации, с целью ее циркуляции через катализатор для подвода или отвода тепла в адиабатическом реакторе, превращения содержащихся в ней непредельных углеводородов и увеличения межрегенерационного пробега катализатора, технологически обвязанную с реактором нагревательную, теплообменную, сепарирующую, емкостную и нагнетательную аппаратуру для нагревания сырья, охлаждения, частичной конденсации, сепарации и ректификации продуктов реакции. При этом в качестве потока сырья используют также изобутан, который предварительно нагретый может подаваться один и/или в смеси с кислородсодержащими соединениями С-Си/или в смеси с олефинсодержащим сырьем, содержащим в своем составе олефины С-С, как на вход в реакционную часть изотермического ...