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27-01-2005 дата публикации

УСТАНОВКА ТЕРМОМЕХАНИЧЕСКОГО КРЕКИНГА И ГИДРОГЕНИЗАЦИИ УГЛЕВОДОРОДОВ

Номер: RU0000043545U1
Автор: Ольховский Э.В.
Принадлежит: Общество с ограниченной ответственностью "Новые технологии бизнеса"

Установка термомеханического крекинга и гидрогенизации углеводородов, включающая бункер исходного материала и реактор, соединенные питающим устройством, отличающаяся тем, что реактор снабжен по меньшей мере одним излучателем акустических колебаний, связанным с генератором указанных колебаний. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 43 545 (13) U1 (51) МПК C10G 47/30 (2000.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ПОЛЕЗНОЙ МОДЕЛИ К ПАТЕНТУ (21), (22) Заявка: 2004127084/22 , 13.09.2004 (24) Дата начала отсчета срока действия патента: 13.09.2004 (45) Опубликовано: 27.01.2005 (73) Патентообладатель(и): Общество с ограниченной ответственностью "НОВЫЕ ТЕХНОЛОГИИ БИЗНЕСА" (RU) U 1 4 3 5 4 5 R U Ñòðàíèöà: 1 U 1 Формула полезной модели Установка термомеханического крекинга и гидрогенизации углеводородов, включающая бункер исходного материала и реактор, соединенные питающим устройством, отличающаяся тем, что реактор снабжен по меньшей мере одним излучателем акустических колебаний, связанным с генератором указанных колебаний. 4 3 5 4 5 (54) УСТАНОВКА ТЕРМОМЕХАНИЧЕСКОГО КРЕКИНГА И ГИДРОГЕНИЗАЦИИ УГЛЕВОДОРОДОВ R U Адрес для переписки: 197136, Санкт-Петербург, а/я 55, пат.пов. Ю.В. Рыбакову, рег.№ 244 (72) Автор(ы): Ольховский Э.В. (RU) U 1 U 1 4 3 5 4 5 4 3 5 4 5 R U R U Ñòðàíèöà: 2 RU 5 10 15 20 25 30 35 40 45 50 43 545 U1 Полезная модель относится к термомеханическому крекингу и гидрогенизации химических веществ. Известны установки термомеханического крекинга и гидрогенизации углеводородов в жидкой или твердой форме, карбонатов, извести, нефтеносных сланцев и песков, маслянистых остатков нефтеперерабатывающих заводов и т.п. Наиболее близким по технической сущности к заявляемой полезной модели является устройство, описанное в патенте РФ, включающее бункер исходного материала и реактор, соединенные питающим устройством (1). Однако, КПД указанного устройства недостаточен. Задачей полезной модели является обработка углеродистого ...

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Номер записи: 1
20-03-2014 дата публикации

УСТАНОВКА ДЛЯ ПЕРЕРАБОТКИ НЕФТЕШЛАМОВ

Номер: RU0000138715U1
Автор: Зайченко Владимир Николаевич
Принадлежит: Зайченко Владимир Николаевич

Установка для переработки нефтешламов, включающая сообщенные между собой устройство для обработки исходного сырья, устройство выделения конечных продуктов, соединенного с устройством для охлаждения и конденсации конечного продукта, отличающаяся тем, что устройство для обработки исходного сырья выполнено из трех, соединенных между собой диафрагм с разным диаметром сечений, на выходе которых установлен полый шар, в котором закреплен металлический шар, а устройство для выделения конечных продуктов состоит из блока подготовки, фильтров-адсорберов, каталитического реактора, источника водяного пара, причем блок подготовки выполнен в виде горизонтального расположенного тора, внутри которого установлены ребра, параллельно боковым стенкам, по всей длине корпуса, вход которого соединен с устройством для обработки исходного сырья и источником водяного пара, а выход с фильтрами-адсорберами, состоящими из корпуса, чугунного и керамического наполнителя, расположенного слоями друг за другом, под днищем которых расположены термостатические рубашки, выходы фильтров-адсорберов соединены с противоположно направленными входами каталитического реактора, который соединен с источником водяного пара. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 138 715 U1 (51) МПК C10G 47/32 (2006.01) C10G 47/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ПОЛЕЗНОЙ МОДЕЛИ К ПАТЕНТУ 2013147315/04, 22.10.2013 (24) Дата начала отсчета срока действия патента: 22.10.2013 (72) Автор(ы): Зайченко Владимир Николаевич (RU) (73) Патентообладатель(и): Зайченко Владимир Николаевич (RU) R U Приоритет(ы): (22) Дата подачи заявки: 22.10.2013 (45) Опубликовано: 20.03.2014 Бюл. № 8 1 3 8 7 1 5 R U Формула полезной модели Установка для переработки нефтешламов, включающая сообщенные между собой устройство для обработки исходного сырья, устройство выделения конечных продуктов, соединенного с устройством для охлаждения и конденсации конечного продукта, отличающаяся тем, что устройство ...

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Номер записи: 2
20-11-2016 дата публикации

Каталитический картридж для осуществления гетерогенных каталитических реакций

Номер: RU0000166263U1
Автор: Андрей Николаевич Загоруйко, Данил Александрович Писарев, Дмитрий Васильевич Баранов, Павел Евгеньевич Микенин, Сергей Алексеевич Лопатин, Сергей Валерьевич Зажигалов
Принадлежит: Федеральное государственное бюджетное учреждение науки Институт катализа им. Г.К. Борескова Сибирского отделения Российской академии наук

1. Каталитический картридж для осуществления гетерогенных каталитических реакций с катализатором, состоящим из нитей, скрученных из каталитических микроволокон, отличающийся тем, что картридж содержит более чем один каталитический элемент, каждый из которых выполнен из каталитической нити с толщиной от 0.1 мм до 5 мм в форме петли, либо другой фигуры, включающей петлю.2. Каталитический картридж по п. 1, отличающийся тем, что каждый каталитический элемент содержит два плоских опорных полотна, расположенных параллельно друг другу на расстоянии от 1 мм до 50 мм и скрепленных между собой регулярно расположенными каталитическими элементами из каталитических нитей в форме петель или других фигур, включающих петлю.3. Каталитический картридж по п. 2, отличающийся тем, что плоские опорные полотна выполнены в форме тканых или плетеных полотен из нитей микроволокнистого катализатора.4. Каталитический картридж по п. 1, отличающийся тем, что каталитические микроволокна представляют собой стеклянные, металлические, минеральные, углеродные, полимерные или иные волокна диаметром от 1 мкм до 30 мкм, на поверхности которых находятся каталитически активные компоненты.5. Каталитический картридж по п. 4, отличающийся тем, что на поверхности микроволокон может находиться дополнительный слой вторичного носителя с развитой внутренней поверхностью, например, слой диоксида кремния, оксида алюминия, диоксида титана или активированного углерода.6. Каталитический картридж по п. 5, отличающийся тем, что в качестве активных компонентов на поверхности микроволокон он содержит благородные металлы, такие как: платина, палладий, золото, серебро и/или оксиды переходных металлов: РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 166 263 U1 (51) МПК B01J 8/00 (2006.01) B01J 35/06 (2006.01) B01J 21/00 (2006.01) B01J 23/00 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ТИТУЛЬНЫЙ (21)(22) Заявка: ЛИСТ ОПИСАНИЯ ПОЛЕЗНОЙ МОДЕЛИ К ПАТЕНТУ 2016109690/04, 17.03.2016 (24) Дата начала отсчета срока ...

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Номер записи: 3
12-03-2018 дата публикации

ТРУБЧАТАЯ ПЕЧЬ КОНВЕКЦИОННОГО НАГРЕВА ТЕПЛОНОСИТЕЛЯ С ПРИНУДИТЕЛЬНОЙ РЕЦИРКУЛЯЦИЕЙ ДЫМОВЫХ ГАЗОВ

Номер: RU0000177784U1
Автор: Семин Артем Валерьевич
Принадлежит: Общество с ограниченной ответственностью "Бантер Групп"

Полезная модель относится к устройствам для нагрева теплоносителей (жидкостей, газов и других), конкретно к трубчатым печам и может быть использована в нефтяной, газовой, нефтеперерабатывающей и нефтехимической отраслях промышленности. Технический результат заявляемой полезной модели заключается в увеличении срока службы устройства за счет устранения воздействия пламени горелочного узла на стенки камеры сгорания, устранения перегрева стенок теплообменной камеры за счет введения камеры смешения и устранения перегрева трубного змеевика благодаря улучшению теплопередачи от горелочного узла к содержимому трубного змеевика за счет использования оребренных труб с внутренними турбулизирующими вставками, при снижении теплопотерь. Указанный технический результат достигается тем, что трубчатая печь содержит корпус с размещенной внутри камерой сгорания, снабженной горелочным узлом, и теплообменной камерой, снабженной по крайней мере одним трубным змеевиком; рециркуляционный вентилятор, вход которого соединен с выходом теплообменной камеры, согласно решению печь содержит камеру смешения, вход которой соединен с выходом камеры сгорания и выходом рециркуляционного вентилятора, а выход соединен с входом теплообменной камеры, камера смешения выполнена из двух концентрических обечаек, между которыми расположено спиральное ребро жесткости, образующее воздушный канал от выхода камеры смешения к входу камеры смешения; печь содержит дутьевой вентилятор, выход которого соединен с воздушным каналом у выхода камеры смешения; горелочный узел снабжен входом для воздуха, соединенным с воздушным каналом у входа камеры смешения; камера сгорания, камера смешения и теплообменная камера расположены в корпусе так, чтобы обеспечить направление потока газа в теплообменной камере под углом 90° относительно направления потока газа в камерах сгорания и смешения. Трубный змеевик выполнен из гладких или оребренных труб и снабжен внутренними турбулизирующими вставками в наиболее теплонапряженных зонах ...

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Номер записи: 4
19-04-2012 дата публикации

Process for producing middle distillates by hydroisomerization and hydrocracking of a heavy fraction derived from a fischer-tropsch effluent

Номер: US20120091034A1
Автор: Aurelie Dandeu, Vincent Coupard
Принадлежит: Eni Spa, IFP Energies Nouvelles IFPEN

The present invention describes a process for producing middle distillates from a C5+ liquid paraffinic fraction, termed a heavy fraction, with an initial boiling point in the range 15° C. to 40° C. produced by Fischer-Tropsch synthesis, comprising the following steps in succession: passing said C5+ liquid paraffinic fraction, termed a heavy fraction, over at least one ion exchange resin at a temperature in the range 80° C. to 150° C., at a total pressure in the range 0.7 to 2.5 MPa, at an hourly space velocity in the range 0.2 to 2.5 h −1 ; eliminating at least a portion of the water formed in step a); hydrogenating the unsaturated olefinic type compounds of at least a portion of the effluent derived from step b) in the presence of hydrogen and a hydrogenation catalyst; and hydroisomerization/hydrocracking of at least a portion of the hydrotreated effluent derived from step c) in the presence of hydrogen and a hydroisomerization/hydrocracking catalyst.

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Номер записи: 5
17-05-2012 дата публикации

Hydroconversion multi-metallic catalyst and method for making thereof

Номер: US20120122655A1
Автор: Alexander E. Kuperman, Dennis Dykstra, Theodorus Maesen
Принадлежит: Chevron USA Inc

In a process for forming a bulk hydroprocessing catalyst by sulfiding a catalyst precursor made in a co-precipitation reaction, up to 60% of the metal precursor feeds do not react to form catalyst precursor and end up in the supernatant. In the present disclosure, the metals can be recovered via any of chemical precipitation, ion exchange, electro-coagulation, and combinations thereof to generate an effluent stream containing less than 50 mole % of metal ions in at least one of the metal residuals, and for at least one of the metal residuals is recovered as a metal precursor feed, which can be recycled for use in the co-precipitation reaction. An effluent stream from the process to waste treatment contains less than 50 ppm metal ions.

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Номер записи: 6
24-05-2012 дата публикации

Process for Cracking Heavy Hydrocarbon Feed

Номер: US20120125812A1
Автор: Robert S. Bridges, Sellamuthu G. Chellappan
Принадлежит: EQUISTAR CHEMICALS LP

A process for cracking a heavy hydrocarbon feed comprising a vaporization step, a hydroprocessing step, and a steam cracking step is disclosed. The heavy hydrocarbon feed is passed to a first zone of a vaporization unit to separate a first vapor stream and a first liquid stream. The first liquid stream is passed to a second zone of the vaporization unit and contacted intimately with a counter-current steam produce a second vapor stream and a second liquid stream. The first vapor stream and the second vapor stream are cracked in the radiant section of the steam cracker to produce a cracked effluent. The second liquid stream reacted with hydrogen in the presence of a catalyst to produce a hydroprocessed product. A liquid hydroprocessed product is fed to the vaporization unit.

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Номер записи: 7
21-06-2012 дата публикации

Method of making a catalyst

Номер: US20120157299A1
Автор: Krishniah Parimi, Thien Duyen Thi Nguyen
Принадлежит: ENERGIA TECHNOLOGIES Inc

Presented are one or more aspects and/or one or more embodiments of catalysts, methods of preparation of catalyst, methods of deoxygenation, and methods of fuel production.

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Номер записи: 8
21-06-2012 дата публикации

Methods of deoxygenation and systems for fuel production

Номер: US20120157727A1
Автор: Krishniah Parimi, Thien Duyen Thi Nguyen
Принадлежит: ENERGIA TECHNOLOGIES Inc

Presented are one or more aspects and/or one or more embodiments of catalysts, methods of preparation of catalyst, methods of deoxygenation, and methods of fuel production.

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Номер записи: 9
19-07-2012 дата публикации

Method for upgrading heavy hydrocarbon oil

Номер: US20120181216A1
Автор: Oleg Kozyuk, Paul A. Reinking, Peter Reimers
Принадлежит: Arisdyne Systems Inc

A process for upgrading hydrocarbon oil including mixing hydrocarbon oil with hydrogen gas and heating the hydrogen-enriched hydrocarbon oil before passing the oil through a cavitation apparatus to induce hydrotreating. Hydrotreating is achieved by hydrodynamically generating hydrogen-filled cavitation bubbles and collapsing the bubbles in the hydrocarbon oil under static pressure. The hydrotreating process can increase the API gravity of the hydrocarbon oil and reduce the viscosity of the hydrocarbon oil.

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Номер записи: 10
19-07-2012 дата публикации

Process for isomerizing a feed stream including one or more c4-c6 hydrocarbons

Номер: US20120184793A1
Автор: David J. Shecterle
Принадлежит: UOP LLC

One exemplary embodiment can be a process for isomerizing a feed stream including one or more C4-C6 hydrocarbons. The process may include contacting the feed stream in an isomerization reaction zone with an isomerization catalyst at isomerization conditions to produce an isomerization zone effluent; passing at least a portion of the isomerization zone effluent to a stabilizer zone and recovering a stabilizer overhead stream, a bottom stream, and a stripper feed stream; passing the stripper feed stream to a stripping zone and separating the stripper feed stream into a stripper overhead stream and a stripper bottom stream; and recycling at least a portion of the stripper bottom stream to a deisopentanizer zone and passing a stream from the deisopentanizer zone to the isomerization reaction zone. Usually, the stabilizer overhead stream includes one or more C5 − hydrocarbons, the bottom stream includes at least about 85%, by weight, one or more C6 + hydrocarbons, and a stripper feed stream including at least about 10%, by weight, one or more C5 + hydrocarbons. Often, a stripper overhead stream includes at least about 5%, by weight, one or more C4 − hydrocarbons and a stripper bottom stream includes at least about 90%, by weight, one or more C5 + hydrocarbons.

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Номер записи: 11
26-07-2012 дата публикации

Molecular Sieve Of MFS Framework Type With Controllable Average Size, Its Method of Making And Use

Номер: US20120190896A1
Автор: Machteld Maria Wilfried Mertens
Принадлежит: ExxonMobil Chemical Patents Inc

A method of making a crystalline molecular sieve of MFS framework type, preferably ZSM-57, from a synthesis mixture comprising at least one source of tetravalent element (Y), at least one source of trivalent element (X), at least one source of alkali metal hydroxide (MOH), at least one structure-directing-agent (R) and water, said alkali metal (M) comprising potassium, and having the following mole composition (expressed in terms of oxide): YO 2 :( p )X 2 O 3 :( q )OH − :( r )R:( s )H 2 O, wherein (p) is in the range from 0.005 to 0.05, (q) is in the range from 0.01 to 3, (r) is in the range from 0.03 to 2 and (s) is in the range from 10 to 75 (based on total weight of said synthesis mixture); wherein the crystals of molecular sieve formed having an average diameter (D) of less than or equal to 1.5 micron and an average thickness (T) of less than or equal to 300 nanometers.

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Номер записи: 12
13-12-2012 дата публикации

Apparatus and method for hydroconversion

Номер: US20120315202A1
Автор: Abdenour Kemoun, Bruce Reynolds, Donald L. Kuehne, Steven X. Song
Принадлежит: Chevron Corp

An apparatus is disclosed for the hydroconversion of hydrocarbon feedstock with a hydrogen gas at elevated temperature and pressure with the use of a catalyst. The apparatus is a reactor vessel with a grid plate distributor for improved gas liquid distribution. The distributor comprises a grid plate and a bubble cap assembly with a plurality of tubular risers extending through the grid plate. Each tubular riser has an upper section above the grid plate and a lower section below the grid plate, the lower section terminated with an open bottom end for ingress of the hydrogen gas and hydrocarbon feedstock, the upper section having a closed top terminated with a housing cap. Each tubular riser has at least a vertical slot and a least a side hole sufficiently sized such that in operation, the liquid level in the zone below the grid plate is above the vertical slot and below the side hole opening.

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Номер записи: 13
28-03-2013 дата публикации

PROCESS FOR HYDROCONVERSION OF PETROLEUM FEEDSTOCKS VIA A SLURRY TECHNOLOGY ALLOWING THE RECOVERY OF METALS FROM THE CATALYST AND FROM THE FEEDSTOCK USING A COKING STEP

Номер: US20130075303A1
Автор: HERAUD Jean Philippe, Morel Frédéric, Quignard Alain
Принадлежит: IFP ENERGIES NOUVELLES

A process for hydroconversion of heavy petroleum feedstocks comprising a hydroconversion step of the feedstock in at least one reactor containing a slurry catalyst and allowing the recovery of metals in the unconverted residual fraction, in particular those used as catalysts, The process comprises a hydroconversion step, a gas/liquid separation step, a coking step, a combustion step, a metals extraction step and a step of preparing catalytic solutions which are recycled to the hydroconversion step. 1. Process for hydroconversion of heavy petroleum feedstocks containing metals comprising:a) a step of hydroconversion of the feedstock in at least one reactor containing a slurry catalyst containing at least one metal, and optionally a solid additive,b) a step of separation of the hydroconversion effluent without decompression into a so-called light fraction containing the compounds boiling at a maximum temperature of 500° C. and a residual fraction,b′) optionally a fractionation step comprising a separation under vacuum of said residual fraction as obtained in step b), and a vacuum residue with a high concentration of metals is obtained,c) a step of coking of said residual fraction as obtained in step b) and/or of said vacuum residue as obtained in step b′) making it possible to obtain a solid effluent containing coke,d) a step of combustion of said solid effluent containing coke at a temperature comprised between 200 and 700° C. making it possible to obtain ashes with a high concentration of metals,e) a step of extraction of the metals from the ashes obtained in the combustion step,f) a step of preparation of metallic solution(s) containing at least the metal of the catalyst which is/are recycled(s) as catalyst in the hydroconversion step.2. Process according to in which said so-called light fraction originating from the separation step without decompression is subjected to at least one hydrotreatment and/or hydrocracking step.3. Process according to claim 1 , in which ...

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Номер записи: 14
28-03-2013 дата публикации

Methods for increasing catalyst concentration in heavy oil and/or coal resid hydrocracker

Номер: US20130075304A1
Автор: Yu-Hwa Chang
Принадлежит: Individual

Methods and systems for hydrocracking a heavy oil feedstock include using a colloidal or molecular catalyst (e.g., molybdenum sulfide) and provide for concentration of the colloidal or molecular catalyst within the lower quality materials requiring additional hydrocracking in one or more downstream reactors. In addition to increased catalyst concentration, the inventive systems and methods provide increased reactor throughput, increased reaction rate, and of course higher conversion of asphaltenes and lower quality materials. Increased conversion levels of asphaltenes and lower quality materials also reduces equipment fouling, enables the reactor to process a wider range of lower quality feedstocks, and can lead to more efficient use of a supported catalyst if used in combination with the colloidal or molecular catalyst.

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Номер записи: 15
04-04-2013 дата публикации

HYDROPROCESSING OF HEAVY HYDROCARBON FEEDS USING SMALL PORE CATALYSTS

Номер: US20130081977A1
Автор: Brown Stephen Harold, Cheng Jane Chi-ya, Ho Teh C., Woo Hyung Suk
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Heavy oil feeds are hydroprocessed in the presence of a solvent and in the presence of a catalyst with a median pore size of about 85 Å to about 120 Å under conditions that provide a variety of benefits. The solvent can be an added solvent or a portion of the liquid effluent from hydroprocessing. The processes allow for lower pressure processing of heavy oil feeds for extended processing times or extended catalyst lifetimes be reducing or mitigating the amount of coke formation on the hydroprocessing catalyst. 1. A process for producing a hydroprocessed product , comprising:{'sup': '−1', 'exposing a combined feedstock comprising a heavy oil feed component and a solvent component to a hydroprocessing catalyst comprising a Group VIII non-noble metal and a Group VI metal and having a median pore size of about 85 Å to about 120 Å, under effective hydroprocessing conditions to form a hydroprocessed effluent, the effective hydroprocessing conditions including a total pressure of about 1500 psig (10.3 MPag) or less, a temperature of at least about 360° C., and a liquid hourly space velocity of the fraction of the combined feedstock boiling above 1050° F. (566° C.) of at least about 0.10 hr;'}separating the hydroprocessing effluent to form at least a liquid effluent; andfractionating a first portion of the liquid effluent to form at least a distillate product and a bottoms product, the bottoms product having an ASTM D86 distillation point of at least about 600° F. (316° C.)2. The process of claim 1 , wherein the hydroprocessing catalyst is a bulk catalyst claim 1 , the hydroprocessing catalyst having a median pore size of about 85 Å to about 100 Å.3. The process of claim 1 , wherein the solvent component comprises a recycle component claim 1 , the process further comprising recycling a second portion of the liquid effluent to form the recycle component.4. The process of claim 3 , wherein the ratio of the recycle component to the heavy oil feed component on a weight basis is ...

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Номер записи: 16
04-04-2013 дата публикации

USE OF LOW BOILING POINT AROMATIC SOLVENT IN HYDROPROCESSING HEAVY HYDROCARBONS

Номер: US20130081978A1
Автор: Brown Stephen Harold, Cheng Jane Chi-ya, Ho Teh C., Woo Hyung Suk
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

This invention is directed to a process for producing a hydroprocessed product. The invention is particularly advantageous in that substantially less hydrogen is absorbed during the process relative to conventional hydroprocessing methods. This benefit is achieved by using a particular solvent as a co-feed component. In particular, the solvent component contains at least one single ring aromatic compound and has a relatively low boiling point range compared to the heavy hydrocarbon oil component used as another co-feed component. 1. A process for producing a hydroprocessed product , comprising:sending to a hydroprocessing zone a combined feed comprised of a heavy hydrocarbon oil component, wherein the heavy hydrocarbon oil component has a ASTM D86 10% distillation point of at least 650° F. (343° C.), and a solvent component containing at least one single ring aromatic compound in which the solvent has an ASTM D86 10% distillation point of at least 120° C. (248° F.) and a 90% distillation point of not greater than 300° C. (572° F.); andcontacting the combined feed with a hydroprocessing catalyst in the presence of hydrogen in the hydroprocessing zone to form a hydroprocessed product.2. The process of claim 1 , wherein the heavy hydrocarbon oil component has an initial ASTM D86 boiling point of at least 650° F. (343° C.).3. The process of claim 1 , wherein the heavy hydrocarbon oil component has an ASTM D86 10% distillation point of at least 750° F. (399° C.).4. The process of claim 1 , wherein the heavy hydrocarbon oil component contains at least 0.0001 grams of Ni/V/Fe claim 1 , on a total elemental basis of nickel claim 1 , vanadium and iron.5. The process of claim 1 , wherein the heavy hydrocarbon oil component contains at least 50 wppm elemental nitrogen claim 1 , based on total weight of the heavy hydrocarbon oil component.6. The process of claim 5 , wherein the heavy hydrocarbon oil component contains at least 500 wppm elemental sulfur claim 5 , based on total ...

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Номер записи: 17
04-04-2013 дата публикации

USE OF SUPERCRITICAL FLUID IN HYDROPROCESSING HEAVY HYDROCARBONS

Номер: US20130081979A1
Автор: Brown Stephen Harold, Cheng Jane Chi-ya, Ho Teh C., Woo Hyung Suk
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

This invention is directed to a process for producing a hydroprocessed product. The invention is particularly advantageous in that substantially longer run length can be attained relative to conventional hydroprocessing methods. This benefit is achieved by using a particular solvent as a co-feed component. In particular, the solvent component is comprised of at least one or more supercritical solvent compounds. 1. A process for producing a hydroprocessed product , comprising:sending to a hydroprocessing zone a combined feed comprised of a heavy hydrocarbon oil component, wherein the heavy hydrocarbon oil component has a ASTM D86 10% distillation point of at least 650° F. (343° C.), and a solvent component in which a majority of the solvent is comprised of at least one supercritical hydrocarbon compound having a critical temperature and pressure; andcontacting the combined feed with a hydroprocessing catalyst in the presence of hydrogen at a temperature and pressure above the critical temperature and pressure of the at least one supercritical hydrocarbon compound to form the hydroprocessed product.2. The process of claim 1 , wherein the heavy hydrocarbon oil component has an initial ASTM D86 boiling point of 650° F. (343° C.) or greater.3. The process of claim 1 , wherein the heavy hydrocarbon oil component contains at least 0.0001 grams of Ni/V/Fe claim 1 , on a total elemental basis of nickel claim 1 , vanadium and iron.4. The process of claim 1 , wherein the combined feed is comprised of from 30 wt % to 90 wt % of the heavy hydrocarbon oil component and from 10 wt % to 70 wt % of the solvent component claim 1 , based on total weight of the combined feed.5. The process of claim 1 , wherein the contacting of the combined feed with the hydroprocessing catalyst in the presence of hydrogen is carried out at a hydrogen partial pressure from 550 psig (3792 kPa-g) to 3000 psig (20684 kPa-g).6. The process of claim 1 , wherein the solvent component is comprised of more ...

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Номер записи: 18
02-05-2013 дата публикации

Nozzle Reactor Systems and Methods of Use

Номер: US20130105361A1
Автор: Ard Christopher Daniel, Joshi Mahendra, Salazar Jose Armando
Принадлежит: MARATHON OIL CANADA CORPORATION

A nozzle reactor system for increasing the conversion rate of material feed injected into the nozzle reactor system. The system includes two or more nozzle reactors aligned in parallel. A main stream of material to be upgraded is divided such that one stream is produced for each nozzle reactor in the system. Each nozzle reactor includes an interior reactor chamber and an injection passage and material feed passage that are each in material injecting communication with the interior reactor chamber. Furthermore, the injection passage is aligned transversely to the injection passage. The injection passage is configured to accelerate cracking material passed therethrough to a supersonic speed. The product produced from each of the nozzle reactors is combined into one product stream. 1. A nozzle reactor system comprising:a stream dividing apparatus comprising a first output port and a second output port;a first nozzle reactor having a feed material injection port in fluid communication with the first output port of the stream dividing apparatus, and an ejection end;a second nozzle reactor having a feed material injection port in fluid communication with the second output port of the stream dividing apparatus, and an ejection end; anda mixing apparatus having a first input port in fluid communication with the ejection end of the first nozzle reactor, and a second input port in fluid communication with the ejection end of the second nozzle reactor.2. The nozzle reactor system as recited in claim 1 , wherein: a reactor body having an interior reactor chamber with an injection end and an ejection end;', 'an injection passage mounted in the nozzle reactor in material injecting communication with the interior reactor chamber, the injection passage having (a) an enlarged volume injection section, an enlarged volume ejection section, and a reduced volume mid-section intermediate the enlarged volume injection section and enlarged volume ejection section, (b) a material injection ...

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Номер записи: 19
23-05-2013 дата публикации

SLURRY BED HYDROPROCESSING AND SYSTEM USING FEEDSTOCK CONTAINING DISSOLVED HYDROGEN

Номер: US20130126392A1
Автор: KOSEOGLU Omer Refa
Принадлежит: Saudi Arabian Oil Company

A system and process for conversion of heavy feedstocks in a slurry bed hydroprocessing reactor is provided in which (a) hydrogen gas is dissolved in the liquid feedstock by mixing and/or diffusion, (b) the mixture is flashed to remove and recover any light components and hydrogen, leaving a hydrogen-enriched feedstock. A homogenous and/or heterogeneous catalyst is added to the feedstock upstream of the inlet of the slurry bed hydroprocessing reactor. 1. A process for converting a liquid hydrocarbon feedstock into lower molecular weight hydrocarbon compounds in a slurry bed reactor , the process comprising:a. mixing the liquid hydrocarbon feedstock and an excess of hydrogen gas in a mixing zone under predetermined conditions of temperature and hydrogen partial pressure to dissolve a portion of the hydrogen gas in the liquid hydrocarbon feedstock to produce a mixture of hydrogen-enriched liquid hydrocarbon feedstock and undissolved hydrogen gas;b. introducing the mixture produced in step (a) into a flashing zone under predetermined conditions to separate undissolved hydrogen gas and light hydrocarbon components and recovering a hydrogen-enriched liquid hydrocarbon feedstock;c. introducing the hydrogen-enriched liquid hydrocarbon feedstock into a reaction zone containing at least one slurry bed reactor with at least one catalyst or catalyst precursor and reacting the feedstock to convert at least a portion of the feedstock into lower boiling point hydrocarbons; andd. recovering converted hydrocarbon products from the slurry bed reactor.2. The process of in which at least a portion of unconverted liquid feedstock is recovered from the slurry bed reactor and is recycled to form a portion of the liquid hydrocarbon feedstock.3. The process of in which the at least one catalyst is selected from a liquid homogeneous catalyst precursor and a small particulate heterogeneous catalyst4. The process of in which fresh catalyst is added to the unconverted feedstock upstream of one ...

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Номер записи: 20
23-05-2013 дата публикации

HIGH SURFACE AREA COMPOSITION FOR USE IN THE CATALYTIC HYDROCONVERSION OF A HEAVY HYDROCARBON FEEDSTOCK, A METHOD MAKING SUCH COMPOSITION AND ITS USE

Номер: US20130126393A1
Автор: GINESTRA Josiane Marie-Rose, JR. David Edward, KESTER John George, KOMAR David Andrew, SHERWOOD
Принадлежит: SHELL OIL COMPANY

A catalyst composition that is especially useful in the hydroconversion of pitch, micro carbon residue and sulfur contents of a heavy hydrocarbon feedstock without the excessive formation of sediment. The catalyst composition is a reasonably high surface area composition containing alumina and a low molybdenum content with a high ratio of nickel-to-molybdenum. The catalyst composition further has a unique pore distribution that in combination with the special metals loading provide for good conversion of pitch and micro carbon residue without an excessive yield of sediment. 1. A catalyst composition comprising a molybdenum component in an amount of greater than or equal to 5 wt. % and less than 11 wt. % , with the wt. % being based on the total weight of said catalyst composition and assuming said molybdenum component is in the oxide form (MoO) regardless of its actual form , and a nickel component present in an amount such that said catalyst composition has a weight ratio of said nickel component-to-said molybdenum component exceeding 0.25 , with said weight ratio being computed assuming said nickel component and said molybdenum component are each in the oxide form regardless of their actual forms , and wherein said catalyst composition has a total surface area in the range of from 240 m/g to 360 m/g , a total pore volume in the range of from 0.65 cc/g to 1.1 cc/g and a pore size distribution such that from 11% to 30.5% of the total pore volume is present in macropores of diameter greater than or equal to 250 Å.2. A catalyst composition as recited in claim 1 , having a pore size distribution such that from 50% to 80% of the total pore volume of said catalyst composition is present as pores having diameters in the range of from 55 Å to 115 Å claim 1 , and from 16% to 30% of the total pore volume of said catalyst composition is present in macropores of diameter greater than 500 Å.3. A catalyst composition as recited in claim 2 , wherein more than 20% of the total ...

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Номер записи: 21
23-05-2013 дата публикации

ACTIVATION OF DUAL CATALYST SYSTEMS

Номер: US20130130893A1
Автор: Helton Terry E., Hilbert Timothy L., III William J., Kalyanaraman Mohan, McCarthy Stephen J., Oliveri Christopher G., Tracy, Umansky Benjamin S.
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Methods are provided for liquid phase activation of dewaxing and/or hydrofinishing catalysts that include a molecular sieve or other acidic crystalline support. The methods are compatible with activating the catalysts as part of a catalyst system that also includes a hydrotreating catalyst. 1. A method for activating a catalyst system , comprising:exposing a catalyst system to a first liquid activation feed under effective reducing conditions for at least about 24 hours, the catalyst system including at least one catalyst that comprises a Group VIII non-noble metal on an amorphous support and at least one catalyst that comprises a Group VIII noble metal on an acidic support, the effective reducing conditions including a hydrogen partial pressure of at least about 500 psig (145 MPag) and a temperature of at least about 200° C.; andexposing the catalyst system to a second liquid activation feed under effective sulfiding conditions.2. The method of claim 1 , wherein the catalyst with an amorphous support is a hydrotreating catalyst.3. The method of claim 1 , wherein the catalyst comprising a Group VIII noble metal on an acidic support comprises a dewaxing catalyst with Pt claim 1 , Pd claim 1 , or a combination thereof on a support including a molecular sieve.4. The method of claim 1 , wherein the catalyst comprising a Group VIII noble metal on an acidic support comprises a hydrofinishing catalyst with Pt claim 1 , Pd claim 1 , or a combination thereof on a support comprising an M41S family support.5. The method of claim 1 , wherein the catalyst system is provided in a single reactor.6. The method of claim 1 , wherein first liquid activation feed comprises a distillate boiling range feed with a sulfur content of less than about 100 wppm and a water content of less than about 100 wppm.7. The method of claim 6 , wherein first liquid activation feed has a nitrogen content of less than about 250 wppm.8. The method of claim 1 , wherein the second liquid activation feed ...

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Номер записи: 22
06-06-2013 дата публикации

Process for producing hydrocarbon oil and system for producing hydrocarbon oil

Номер: US20130143971A1
Автор: Kazuhiko Tasaka, Marie Iwama, Yuichi Tanaka
Принадлежит: Cosmo Oil Co Ltd, Inpex Corp, Japan Oil Gas and Metals National Corp, Japan Petroleum Exploration Co Ltd, JX Nippon Oil and Energy Corp, Nippon Steel and Sumikin Engineering Co Ltd

Hydrocarbon oil obtained by Fischer-Tropsch synthesis reaction using a slurry bed reactor holding a slurry of a liquid hydrocarbon in which a catalyst is suspended; the hydrocarbon oil is fractionated into a distilled oil and a column bottom oil containing the catalyst fine powder by a rectifying column; at least part of the column bottom oil is transferred to a storage tank, and the catalyst fine powder is sedimented to the bottom of the storage tank to capture the catalyst fine powder; a residue of the column bottom oil is transferred from the rectifying column to a hydrocracker, and/or the supernatant of the column bottom oil from which the catalyst fine powder is captured by the storage tank is transferred from the storage tank to the hydrocracker; and using the hydrocracker, the residue of the column bottom oil and/or the supernatant of the column bottom oil is hydrocracked.

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Номер записи: 23
11-07-2013 дата публикации

HYDROCRACKING CATALYST FOR HYDROCARBON OIL, METHOD FOR PRODUCING HYDROCRACKING CATALYST, AND METHOD FOR HYDROCRACKING HYDROCARBON OIL WITH HYDROCRACKING CATALYST

Номер: US20130175202A1
Автор: "Al-AbdulAl Ali H.", Al-Hajji Adnan, Al-Somali Ali Mahmood, Al-Thukair Mishaal, Kameoka Takashi, KOSEOGLU Omer Refa, Kuroda Ryuzo, Nakano Koji, Takamori Yuichi, Ushio Masaru
Принадлежит:

The present invention relates to a hydrocracking catalyst for hydrocarbon oil comprising a support containing a framework-substituted zeolite-1 in which zirconium atoms and/or hafnium atoms form a part of a framework of an ultrastable y-type zeolite and a hydrogenative metal component carried thereon and a method for producing the same. The hydrocracking catalyst of the present invention makes it easy to diffuse heavy hydrocarbon oils such as VGO, DAO and the like into mesopores, is improved in a cracking activity and makes it possible to obtain a middle distillate at a high yield as compared with catalysts prepared by using zeolite comprising titanium and/or zirconium carried thereon. 1. A hydrocracking catalyst for hydrocarbon oil comprising a hydrogenative metal component carried on a support containing an ultra-stable Y-type zeolite , wherein the above ultra-stable Y-type zeolite is a framework-substituted zeolite (hereinafter referred to as a framework-substituted zeolite-1) in which a part of aluminum atoms constituting a zeolite framework thereof is substituted with zirconium atoms and/or hafnium atoms.2. A hydrocracking catalyst for hydrocarbon oil according to claim 1 , wherein said zeolite-1 contains from 0.1 to 5 mass % zirconium atoms and/or hafnium atoms as calculated as the oxide basis.3. The hydrocracking catalyst for hydrocarbon oil according to or claim 1 , wherein said zeolite-1 further contains titanium atoms.4. The hydrocracking catalyst for hydrocarbon oil according to claim 3 , wherein in the zeolite-1 claim 3 , a part of the aluminum atoms forming the zeolite framework is further substituted with titanium atoms.5. The hydrocracking catalyst for hydrocarbon oil according to or claim 3 , wherein said zeolite-1 contains from 0.1 to 5 mass % titanium atoms as calculated as the oxide basis.6. The hydrocracking catalyst for hydrocarbon oil according to any of to claim 3 , wherein the support contains the zeolite-1 and inorganic oxide excluding the ...

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Номер записи: 24
18-07-2013 дата публикации

CATALYST FOR USE IN HYDROCONVERSION, COMPRISING AT LEAST ONE ZEOLITE AND METALS FROM GROUPS VIII AND VIB, AND PREPARATION OF THE CATALYST

Номер: US20130180886A1
Автор: DATH Jean Pierre, DE GRANDI Valentina, DULOT Hugues, GUICHARD Bertrand, LAPISARDI Gregory, Minoux Delphine, SIMON Laurent
Принадлежит:

The invention concerns a catalyst containing a support comprising at least one binder and at least one zeolite having at least one series of channels the opening of which is defined by a ring containing 12 oxygen atoms, said catalyst comprising phosphorus, at least one C1-C4 dialkyl succinate, acetic acid and a hydrodehydrogenating function comprising at least one element from group VIB and at least one element from group VIII, the Raman spectrum of the catalyst comprising bands at 990 and/or 974 cm, characteristic of at least one Keggin heteropolyanion, the characteristic bands of said succinate and the characteristic principal band of acetic acid at 896 cm. 1. A catalyst containing a support comprising at least one binder and at least one zeolite having at least one series of channels the opening of which is defined by a ring containing 12 oxygen atoms , said catalyst comprising phosphorus , at least one C1-C4 dialkyl succinate , acetic acid and a hydrodehydrogenating function comprising at least one element from group VIB and at least one element from group VIII , the Raman spectrum of the catalyst comprising bands at 990 and/or 974 cm , characteristic of at least one Keggin heteropolyanion , the characteristic bands of said succinate and the characteristic principal band of acetic acid at 896 cm.2. A catalyst according to claim 1 , in which the dialkyl succinate is dimethyl succinate and in which the Raman spectrum of the catalyst has principal bands at 990 and/or 974 cmwhich are characteristic of Keggin heteropolyanions claim 1 , and at 853 cm claim 1 , which is characteristic of dimethyl succinate and at 896 cm claim 1 , which is characteristic of acetic acid.3. A catalyst according to claim 1 , in which the dialkyl succinate is diethyl succinate claim 1 , dibutyl succinate or diisopropyl succinate.4. A catalyst according to claim 1 , comprising a support constituted by alumina and zeolite.5. A catalyst according to claim 1 , comprising a support constituted ...

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Номер записи: 25
01-08-2013 дата публикации

INTEGRATED SOLVENT DEASPHALTING AND STEAM PYROLYSIS PROCESS FOR DIRECT PROCESSING OF A CRUDE OIL

Номер: US20130197289A1
Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, SAYED Essam, SHAFI Raheel
Принадлежит: Saudi Arabian Oil Company

A process is provided that is directed to a steam pyrolysis zone integrated with a solvent deasphalting zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. The integrated solvent deasphalting and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals comprises charging the crude oil to a solvent deasphalting zone with an effective amount of solvent to produce a deasphalted and demetalized oil stream and a bottom asphalt phase; thermally cracking the deasphalted and demetalized oil stream in the presence of steam to produce a mixed product stream; separating the mixed product stream; recovering olefins and aromatics from the separated mixed product stream; and recovering pyrolysis fuel oil from the separated mixed product stream. 1. An integrated solvent deasphalting and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals , the process comprising:a. charging the crude oil to a solvent deasphalting zone with an effective amount of solvent to produce a deasphalted and demetalized oil stream and a bottom asphalt phase;b. thermally cracking the deasphalted and demetalized oil stream in the presence of steam to produce a mixed product stream;c. separating the thermally cracked mixed product stream;d. recovering olefins and aromatics from the separated mixed product stream; ande. recovering pyrolysis fuel oil from the separated mixed product stream.2. The integrated process of claim 1 , wherein step (c) comprises compressing the thermally cracked mixed product stream with plural compression stages;subjecting the compressed thermally cracked mixed product stream to caustic treatment to produce a thermally cracked mixed product stream with a reduced content of hydrogen sulfide and carbon dioxide;compressing the thermally cracked mixed product stream with a reduced content of hydrogen sulfide and ...

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Номер записи: 26
15-08-2013 дата публикации

INTEGRATED PROCESS FOR UPGRADING HEAVY OIL

Номер: US20130206642A1
Автор: Chung Keng H., Sun Xuewen, Xu Chunming, Xu Zhiming, ZHAO SUOQI
Принадлежит: CHINA UNIVERSITY OF PETROLEUM-BEIJING

The invention provides an integrated process for processing heavy oil, wherein the integrated process at least comprises: solvent deasphalting is carried out for heavy oil material, and de-oiled asphalt phase is mixed with dispersing agent and then entered a thermal cracking reactor to undergo thermal cracking reactions. Upgraded oil can be obtained through the mixture of the de-asphalted oil and thermal cracking oil separated from thermal cracking reaction products. The solvent and heavy gas oil, which are separated from the thermal cracking reaction products, are respectively recycled back to the solvent deasphalting process as solvent and as mixed feed to remove asphaltene. The integrated process of the present invention solves the problems that solvent is difficult to be separated from asphalt with high softening point in solvent deasphalting process and hard asphalt is difficult to be transported. 1. A integrated process for processing heavy oil , comprising at least the following processes , wherein:a heavy oil feedstock, which substantially does not comprise <350° C. atmospheric distillates, is used as feed and subjected to solvent deasphalting process in an extraction tower with an extraction solvent, a de-asphalted oil and a de-oiled asphalt phase including the extraction solvent are collected;the de-oiled asphalt phase including the extraction solvent is mixed with a dispersing solvent and then enters into a thermal cracking reactor to be subjected to a thermal cracking process, so as to obtain thermal cracking reaction product and coke, the thermal cracking reaction product is led out, gas, solvent, thermal cracking oil and 450° C.+ heavy gas oil are separated therefrom;the solvent separated from the thermal cracking product is recycled back to the solvent deasphalting process to be recycled, the 450° C.+ heavy gas oil is recycled back to the solvent deasphalting process to be used as mixed feed;upgraded oil is obtained through mixing the de-asphalted oil ...

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Номер записи: 27
29-08-2013 дата публикации

PROCESS FOR HYDROCRACKING A HYDROCARBON FEEDSTOCK

Номер: US20130220885A1
Автор: Glenn Michael, Low Gordon Gongngai
Принадлежит: Haldor Topsoe A/S

A hydrocracking process comprising the steps of: (a) combining a hydrocarbonaceous feedstock and a heavy bottom fraction recycle stream with a hydrogen-rich gas to obtain a mixture comprising hydrocarbonaceous feedstock and hydrogen; (b) catalytically hydrocracking the mixture comprising hydrocarbonaceous feedstock and hydrogen in a hydrocracking zone to obtain a hydrocracked effluent; (c) separating the hydrocracked effluent into a first vapour portion and a first liquid portion in a separation zone; (d) heating the first liquid portion to form a vapourised first liquid portion; (e) feeding the vapourised first liquid portion to a fractionation section producing individual product fractions including a heavy bottom fraction comprising unconverted oil at the bottom zone of the fractionation section; (f) withdrawing from the fractionation section the heavy bottom fraction; (g) splitting the heavy bottom fraction in a stream for stripping and a heavy bottom fraction recycle stream; (h) stripping the stream for stripping, with a stripping medium, in a counter current stripping column to form an overhead vapour and a stripped liquid; (i) feeding the overhead vapour to the fractionation section, to a recycle stream or to a position upstream the fractionation section; and (j) removing at least a part of the stripped liquid from the counter current stripping column as a net purge of unconverted oil. 1. A hydrocracking process comprising the steps of:(a) combining a hydrocarbonaceous feedstock and a heavy bottom fraction recycle stream with a hydrogen-rich gas to obtain a mixture comprising hydrocarbonaceous feedstock and hydrogen;(b) catalytically hydrocracking the mixture comprising hydrocarbonaceous feedstock and hydrogen in a hydrocracking zone to obtain a hydrocracked effluent;(c) separating the hydrocracked effluent into a first vapour portion and a first liquid portion in a separation zone;(d) heating the first liquid portion to form a vapourised first liquid portion ...

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Номер записи: 28
29-08-2013 дата публикации

METHOD FOR PREPARING HYDROREFINING CATALYST

Номер: US20130225400A1
Автор: Gong Guangbi, Huang Dehua, Jiang Cailan, Kang Hongmin, Liang Shunqin, Lv Longgang, SUN LIMIN, Wang Shufeng, Wang Tinghai, Wang Zongbao, Wu Jie, XIE Wei, Xue Huifeng, Zheng Yundi
Принадлежит: PETROCHINA COMPANY LIMITED

A method for preparing hydrorefining catalyst comprises the following steps: (1) mixing an aqueous ammonia solution with a polyamine complexing agent to form a mixed solvent; (2) adding a cobalt salt to the mixed solvent, dissolving the cobalt salt, and then adding a molybdenum salt and optional salts of other active components, and dissolving them to prepare an impregnating solution; and (3) impregnating a support with the impregnating solution, followed by aging, drying, and activating the impregnated support to form a hydrorefining catalyst. The hydrorefining catalyst prepared by this method has good activity, selectivity and stability in use. 1. A method for preparing hydrorefining catalyst , comprising:supporting active components on a support, the active components comprising cobalt and molybdenum, wherein mixing an aqueous ammonia with a polyamine complexing agent to form a mixed solvent;adding a salt comprising the active component cobalt to the mixed solvent, dissolving the cobalt salt, and then adding a molybdenum salt or a molybdenum salt and salts of other active components and promoters, and dissolving them to prepare an impregnation solution; andimpregnating a support with the impregnating solution, followed by aging, drying and activating the impregnated support to obtain the hydrorefining catalyst.2. The method for preparing hydrorefining catalyst according to claim 1 , wherein a nickel salt claim 1 , a tungsten salt and/or a soluble alkali or carbonate compound of a Group IA element is added during formulation of the impregnation solution.3. The method for preparing hydrorefining catalyst according to claim 1 , wherein the impregnation solution has a pH value of above 10 claim 1 ,4. The method for preparing hydrorefining catalyst according to claim 1 , wherein the polyamine complexing agent is one or more of EDTA claim 1 , triethylene tetramine claim 1 , triethanolamine and ethylenediamine.5. The method for preparing hydrorefining catalyst according ...

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Номер записи: 29
05-09-2013 дата публикации

Method for efficiently operating an ebbulated bed reactor and an efficient ebbulated bed reactor

Номер: US20130228494A1
Автор: Lap Keung Lee, Roger K. Lott
Принадлежит: Headwaters Heavy Oil LLC

A hydroprocessing method and system involves introducing heavy oil and well-dispersed metal sulfide catalyst particles, or a catalyst precursor capable of forming the well-dispersed metal sulfide catalyst particles in situ within the heavy oil, into a hydroprocessing reactor. The well-dispersed or in situ metal sulfide catalyst particles are formed by 1) premixing a catalyst precursor with a hydrocarbon diluent to form a precursor mixture, 2) mixing the precursor mixture with heavy oil to form a conditioned feedstock, and 3) heating the conditioned feedstock to decompose the catalyst precursor and cause or allow metal from the precursor to react with sulfur in the heavy oil to form the well-dispersed or in situ metal sulfide catalyst particles. The well-dispersed or in situ metal sulfide catalyst particles catalyze beneficial upgrading reactions between the heavy oil and hydrogen and eliminates or reduces formation of coke precursors and sediment.

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Номер записи: 30
05-09-2013 дата публикации

INTEGRATED SOLVENT DEASPHALTING AND STEAM PYROLYSIS PROCESS FOR DIRECT PROCESSING OF A CRUDE OIL

Номер: US20130228496A1
Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, SAYED Essam, SHAFI Raheel
Принадлежит: Saudi Arabian Oil Company

A process is provided that is directed to a steam pyrolysis zone integrated with a solvent deasphalting zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. The integrated solvent deasphalting and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals comprises charging the crude oil to a solvent deasphalting zone with an effective amount of solvent to produce a deasphalted and demetalized oil stream and a bottom asphalt phase; thermally cracking the deasphalted and demetalized oil stream in the presence of steam to produce a mixed product stream; separating the mixed product stream; recovering olefins and aromatics from the separated mixed product stream; and recovering pyrolysis fuel oil from the separated mixed product stream. 1. An integrated solvent deasphalting and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals , the process comprising:a. charging the crude oil to a solvent deasphalting zone with an effective amount of solvent to produce a deasphalted and demetalized oil stream and a bottom asphalt phase;b. thermally cracking the deasphalted and demetalized oil stream in the presence of steam to produce a mixed product stream;c. separating the thermally cracked mixed product stream;d. recovering olefins and aromatics from the separated mixed product stream; ande. recovering pyrolysis fuel oil from the separated mixed product stream.2. The integrated process of claim 1 , wherein step (c) comprisescompressing the thermally cracked mixed product stream with plural compression stages;subjecting the compressed thermally cracked mixed product stream to caustic treatment to produce a thermally cracked mixed product stream with a reduced content of hydrogen sulfide and carbon dioxide;compressing the thermally cracked mixed product stream with a reduced content of hydrogen sulfide and ...

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Номер записи: 31
03-10-2013 дата публикации

Hydrocarbon conversion process

Номер: US20130256190A1
Автор: Mark Van Wees, Robert Haizmann
Принадлежит: UOP LLC

One exemplary embodiment can be a process for hydrocarbon conversion. The process can include providing a feed to a slurry hydrocracking zone, obtaining a hydrocarbon stream including one or more C16-C45 hydrocarbons from the at least one separator, providing another feed to a hydrocracking zone, and providing hydrogen from a three-stage compressor to the slurry hydrocracking zone and the hydrocracking zone. Moreover, the slurry hydrocracking zone may include a slurry hydrocracking reactor and at least one separator.

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Номер записи: 32
31-10-2013 дата публикации

HYDROCRACKING PROCESS OF HEAVY HYDROCARBON DISTILLATES USING SUPERCRITICAL SOLVENT

Номер: US20130284639A1
Автор: Choi Sun, Jeong IL Yong, Kim Do Woan, Kim Eun Kyoung, Kim Gyung Rok, Kim Yo Han, LEE Chang Ha, Lee Jae Hyuk, PARK Sung Bum, Ryu Jae Wook
Принадлежит:

Specific embodiments of the present invention provide a hydrocracking process for converting low value-added heavy hydrocarbon distillates into high value-added hydrocarbon distillates using a supercritical solvent as a medium. 1. A method of converting a heavy hydrocarbon distillate into a low-boiling hydrocarbon , the method comprising the step of:contacting a heavy hydrocarbon distillate with a supercritical xylene-containing solvent in the presence of a hydrogenation catalyst to hydrogenate the heavy hydrocarbon distillate for converting the heavy hydrocarbon distillate into the low-boiling hydrocarbon.2. The method of claim 1 , wherein the hydrogenation of the heavy hydrocarbon distillate is performed at a hydrogen pressure of 30 to 150 bars.3. The method of claim 1 , wherein the supercritical xylene-containing solvent is an aromatic solvent comprising at least 25 wt % of m-xylene.4. The method of claim 3 , wherein the supercritical xylene-containing solvent comprises (i) 70 to 85 wt % of xylene claim 3 , (ii) 15 to 25 wt % of ethylbenzene claim 3 , and (iii) 5 wt % of toluene or a C+ aromatic.5. The method of claim 1 , wherein the heavy hydrocarbon distillate is a vacuum residue.6. The method of claim 1 , wherein a weight ratio of the supercritical xylene-containing solvent to the heavy hydrocarbon distillate (xylene-containing solvent/heavy hydrocarbon distillate) is 3 to 10.7. The method of claim 1 , wherein the hydrogenation of the heavy hydrocarbon distillate is performed at a temperature of 350° C. to 420° C. and a hydrogen pressure of 30 to 100 bars.8. The method of claim 1 , wherein the hydrogenation catalyst comprises one of a metal-based catalyst and an active carbon catalyst.9. The method of claim 8 , wherein the metal-base catalyst comprises Mo claim 8 , W claim 8 , Co claim 8 , Ni or a combination thereof.10. The method of claim 8 , wherein the active carbon catalyst is an acid-treated active carbon catalyst.11. The method of claim 10 , wherein the ...

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Номер записи: 33
31-10-2013 дата публикации

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

Номер: US20130289325A1
Автор: Masahide Kobayashi, Ryoji Ida, Shinichiro Yanagawa, Yasuyuki Iwasa
Принадлежит: JX Nippon Oil and Energy Corp

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

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Номер записи: 34
07-11-2013 дата публикации

MESOSTRUCTURED ZEOLITIC MATERIALS SUITABLE FOR USE IN HYDROCRACKING CATALYST COMPOSITIONS AND METHODS OF MAKING AND USING THE SAME

Номер: US20130292300A1
Автор: Garcia-Martinez Javier, Ying Jackie Y.
Принадлежит:

Hydrocracking processes and catalyst composition for use therein are provided. The catalyst compositions described herein include a mesoporous support material and at least one catalytic metal supported thereon. The mesoporous support material may comprise a single-phase crystalline mesostructured zeolite. Additionally, the mesoporous structure may exhibit long range crystallinity and include a plurality of mesopores defined within of the volume of the crystalline mesostructure. Suitable feedstocks for the hydrocracking processes according to embodiments of the present invention crude oil, a gas oil fraction, vacuum gas oil, and combinations thereof. 1. A hydrocracking process comprising: contacting said hydrocarbon-containing feedstock with a catalyst composition under hydrocracking conditions to thereby produce a hydrocracked product , wherein said catalyst composition comprises a mesoporous support material and at least one catalytic metal supported thereon , wherein said mesoporous support material comprises a mesostructured crystalline inorganic one-phase hybrid single crystal material having long-range crystallinity and comprising a plurality of mesopores.2. The hydrocracking process of claim 1 , wherein said crystalline inorganic material is a zeolite.3. The hydrocracking process of claim 1 , wherein said mesopores are configured in an arranged pattern claim 1 , wherein the arranged pattern produces one or more distinctive XRD peaks at two theta values between 0 and 8 two theta angle degrees and one or more distinctive XRD peaks at two theta values between 0 and 8 two theta angle degrees higher than 8.4. The hydrocracking process of claim 1 , wherein said crystalline inorganic material has the structure of a faujasite (FAU) claim 1 , mordenite (MOR) claim 1 , or ZSM-5 (MFI).5. The hydrocracking process of claim 1 , wherein said crystalline inorganic material has a total mesoporous adsorption volume of at least 0.05 cubic centimeters per gram (cc/g).6. The ...

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Номер записи: 35
14-11-2013 дата публикации

METHOD OF PREPARING A HYDROCONVERSION CATALYST BASED ON SILICA OR SILICA-ALUMINA HAVING AN INTERCONNECTED MESOPOROUS TEXTURE

Номер: US20130299388A1
Автор: Bulut Metin, Dath Jean-Pierre, Fajula Francois, Finiels Annie, Hulea Vasile, Kenmogne-Gatchuissi Régine, Van Donk Sander
Принадлежит:

The invention relates to a method for preparing a hydroconversion catalyst based on mesoporous silica or silica-alumina, comprising the following steps: 1. Method for preparing a hydroconversion catalyst based on mesoporous silica or silica-alumina , comprising the following steps:(A) deposition of alumina on a mesoporous material having interconnected pores by treatment with at least one aluminium-based reactant, so as to obtain a compound having a Si/Al ratio of between 0.1 and 1000;(B) addition of at least one catalytically active species chosen from the group formed by the metals of group VIII and/or of group VIB; and(C) drying followed by thermal and/or chemical treatment,2. Method of preparation according to claim 1 , in which the aluminium-based reactant of step (A) is chosen from AlCl claim 1 , NaAlO claim 1 , Al(NO)and Al(OR)where R is chosen from linear or branched C-Calkyl groups.3. Method of preparation according to claim 1 , in which step (B) further includes the addition of one or more dopant metals chosen from the group of rare earths or from group IVB or IB and/or the addition of one or more other dopant elements for example chosen from chlorine claim 1 , fluorine claim 1 , boron and phosphorus.4. Method of preparation according to claim 3 , in which the one or more dopant metals are Ti and/or Cu.5. Method of preparation according to claim 1 , in which step (A) is a step of grafting Al(OR)groups onto a silica or silica-alumina having interconnected mesoporosity claim 1 , in which R is chosen from linear or branched C-Calkyl groups.6. Method of preparation according to claim 5 , in which step (A) of grafting Al(OR)groups comprises:{'sub': 3', '1', '6, '(i) reaction of the mesostructured silica or silica-alumina, with an aluminium-containing compound of formula Al(OR)in which R is chosen from linear or branched C-Calkyl groups, in the presence of an activation agent for activating the protons of the silanol groups of the silica in a solvent, the water ...

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Номер записи: 36
28-11-2013 дата публикации

Process for direct hydrogen injection in liquid full hydroprocessing reactors

Номер: US20130313161A1
Автор: Hasan Dindi
Принадлежит: EI Du Pont de Nemours and Co

A process of hydroprocessing a hydrocarbon in a down flow reactor comprising one or more hydroprocessing-catalyst beds. The hydrocarbon feed is mixed with hydrogen and optionally diluent to form a liquid feed mixture wherein hydrogen is dissolved in the mixture, and the liquid feed mixture is introduced into the down flow reactor under hydroprocessing conditions. The hydroprocessing-catalyst bed(s) are liquid-full and the feed reacts by contact with the catalyst. Hydrogen gas is injected into at least one of the hydroprocessing-catalyst beds such that at least part of the hydrogen consumed in that bed is replenished and the liquid-full condition is maintained. In a multi-bed reactor, hydrogen gas may be injected into more than one or all of the hydroprocessing-catalyst beds.

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Номер записи: 37
28-11-2013 дата публикации

PETROLEUM UPGRADING AND DESULFURIZING PROCESS

Номер: US20130313162A1
Автор: Aljishi Mohammad F., Choi Ki-Hyouk
Принадлежит: Saudi Arabian Oil Company

A petroleum feedstock upgrading method is provided. The method includes supplying a mixed stream that includes hydrocarbon feedstock and water to a hydrothermal reactor where the mixed stream is maintained at a temperature and pressure greater than the critical temperatures and pressure of water in the absence of catalyst for a residence time sufficient to convert the mixed stream into a modified stream having an increased concentration of lighter hydrocarbons and/or concentration of sulfur containing compounds. The modified stream is then supplied to an adsorptive reaction stage charged with a solid adsorbent operable to remove at least a portion of the sulfur present to produce a trimmed stream. The trimmed stream is then separated into a gas and a liquid streams, and the liquid stream is separated into a water stream and an upgraded hydrocarbon product stream. 1. A method for upgrading a petroleum feedstock without supplying an external hydrogen gas supply , the method comprising the steps of:supplying a petroleum feedstock to a mixer, where the step includes pumping the petroleum feedstock to a pressure greater than 22.06 MPa and heating the petroleum feedstock to a temperature of up to about 250° C. to produce a pressurized and heated petroleum feedstock,supplying a water feed to a mixer, where the step includes pumping the water feed to a pressure greater than 22.06 MPa and heating the water feed to a temperature of between about 250° C. and 650° C. to produce a pressurized and heated water feed;combining the heated and pressurized petroleum feedstock and the heated and pressurized water feed in the mixer to produce a pressurized and heated combined stream;supplying the pressurized and heated combined stream to a hydrothermal reactor, where the hydrothermal reactor is maintained at a temperature between about 380° C. and 550° C. and where the pressurized and heated combined stream is maintained in a reaction zone of the hydrothermal reactor for a hydrothermal ...

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Номер записи: 38
28-11-2013 дата публикации

PURGE/SAMPLING SYSTEM FOR A VESSEL, THE CORRESPONDING VESSEL AND CLEANING METHOD USING SAID PURGE/SAMPLING SYSTEM

Номер: US20130313163A1
Автор: Le Lannic Katell, Mourain Xavier, Varin Maxime
Принадлежит: TOTAL RAFFINAGE MARKETING

The invention concerns a purge/sampling system for vessels, particularly for high temperature, high pressure vessels such as hydroconversion reactors used in refinery processes and operated in severe conditions. 1161820221624. Purge/sampling system for a vessel , comprising a purge/sampling line () equipped with a connector designed to be connected to the vessel , a first () and a second () flow regulation systems mounted in series on the purge/sampling line , wherein at least one injection line () is connected to the purge/sampling line () between the first and the second flow regulation systems , said injection line comprising connecting means to a source of cleaning fluid () and at least one flow regulation device to control the flow of cleaning fluid through injection line and purge/sampling line , and wherein the first and second flow regulation systems each comprise at least two control valves in series.22829. Purge/sampling system according to claim 1 , wherein said injection line comprises at least one check valve ( claim 1 , ) to impede the cleaning fluid to flow toward the source of cleaning fluid.3. Purge/sampling system according to claim 2 , wherein said injection line comprises at least two check valves in series.4. Purge/sampling system according to claim 1 , wherein the at least two control valves in series of the first and second flow regulation systems and/or the at least two check valves in series of the injection line are valves of different technology.5. Purge/sampling system according to claim 1 , wherein the control valves in series of the first and second flow regulation systems are two-way control valves.6. Purge/sampling system according to claim 1 , wherein the control valves in series of the first and second flow regulation systems and/or the check valve(s) of the injection line are air operating valves.7. Purge/sampling system according to claim 1 , wherein the control valves in series of the first and second flow regulation systems and/ ...

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Номер записи: 39
19-12-2013 дата публикации

PROCESS FOR THE HYDROCRACKING OF HYDROCARBON CUTS USING A CATALYST BASED ON HETEROPOLYANIONS TRAPPED IN A MESOSTRUCTURED OXIDE SUPPORT

Номер: US20130334099A1
Автор: Bader Manuela, Bonduelle Audrey, Chaumonnot Alexandra, Dufaud Veronique, Lefebvre Frederic, Lopes Silva Susana, Marchand Karin
Принадлежит:

A process for the hydrocracking a hydrocarbon-containing feedstock in which at least 50% by weight of the compounds have an initial boiling point above 340° C. and a final boiling point below 540° C., using a catalyst having, in its oxide form, at least one metal selected from the metals of groups VIB, VIII and VB, said metals being present in the form of at least one polyoxometallate of formula (HXMO), said polyoxometallates being present within a mesostructured matrix based on oxide of at least one element Y, said matrix having a pore size between 1.5 and 50 nm and having amorphous walls of thickness between 1 and 30 nm, said catalyst being sulphurized before used in said process. 1. Process for the hydrocracking of at least one hydrocarbon-containing feedstock , in which at least 50% by weight of the compounds have an initial boiling point above 340° C. and a final boiling point below 540° C. , using a catalyst comprising , in its oxide form , at least one metal selected from the metals of group VIB , the metals of group VIII and the metals of group VB of the periodic table , used alone or in a mixture , said metals being present in the form of at least one polyoxometallate of formula (HXMO) in which X is an element selected from phosphorus (P) , silicon (Si) , boron (B) , nickel (Ni) and cobalt (Co) , said element being used alone , M is one or more element(s) selected from vanadium (V) , niobium (Nb) , tantalum (Ta) , molybdenum (Mo) , tungsten (W) , nickel (Ni) and cobalt (Co) , O is oxygen , H is hydrogen , h is an integer comprised between 0 and 12 , x is an integer comprised between 0 and 4 , m is an integer equal to 5 , 6 , 7 , 8 , 9 , 10 , 11 , 12 or 18 , y is an integer comprised between 17 and 72 and q is an integer comprised between 1 and 20 , said polyoxometallates being present within a mesostructured matrix based on oxide of at least one element Y selected from the group constituted by silicon , aluminium , titanium , zirconium , gallium , and ...

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Номер записи: 40
19-12-2013 дата публикации

BULK CATALYST COMPOSITION COMPRISING BULK METAL OXIDE PARTICLES

Номер: US20130337996A1
Автор: Eijsbouts-Spickova Sona, Lebens Paul Joseph Maria, LELIVELD Robertus Gerardus, Miseo Sabato, Oogjen Bob Gerardus, Plantenga Frans Lodewijk, Soled Stuart Leon, Tromp Henk Jan
Принадлежит: Albemarle Netherlands B.V.

The invention relates to a process for preparing bulk metal oxide particles comprising the steps of combining in a reaction mixture (i) dispersible nanoparticles having a dimension of less than about 1 μm upon being dispersed in a liquid, (ii) at least one Group VIII non-noble metal compound, (iii) at least one Group VIB metal compound, and (iv) a protic liquid; and reacting the at least one Group VIII non-noble metal compound and the at least one Group VIB metal in the presence of the nanoparticles. It also relates to bulk metal hydroprocessing catalysts obtainable by such method. 1. A process for preparing bulk metal oxide particles comprising the steps of combining in a reaction mixture (i) dispersible nanoparticles having a dimension of less than about 1 μm upon being dispersed in a liquid , (ii) at least one Group VIII non-noble metal compound , (iii) at least one Group VIB metal compound , and (iv) a protic liquid; and reacting the at least one Group VIII non-noble metal compound and the at least one Group VIB metal in the presence of the nanoparticles , wherein said nanoparticles are different in composition from said at least one Group VIII non-noble metal compound and said at least one Group VIB metal compound.2. The process according to claim 1 , wherein the nanoparticles are clay mineral particles.3. The process according to or claim 1 , wherein at least one Group VIII non-noble metal compound and at least two Group VIB metal compounds are combined in the reaction mixture.4. The process according to any one of or claim 1 , wherein the reaction mixture further comprises a Group V metal compound.5. The process according to any one of or claim 1 , wherein the metal compounds are at least partly in the solid state during the process.6. The process according to any one of or claim 1 , wherein the nanoparticles are added to the reaction mixture after the metal compounds.8. The process according to claim 7 , wherein the at least one Group VIII non-noble metal ...

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Номер записи: 41
09-01-2014 дата публикации

Integrating An Atmospheric Fractionator With A Diluent Recovery Unit And A Resid Hydrocracker

Номер: US20140008268A1
Автор: Cantley Gregory A., Keppers Dennis W.
Принадлежит: MARATHON PETROLEUM COMPANY LP

This is a unique way to optimize an existing refinery to process heavy bitumen. The upgrade utilizes a diluent recovery unit (DRU) in front of a Resid Hydrocracker. The recovered bitumen from the Resid Hydrocracker is fed to an integrated atmospheric fractionator to convert the light sweet refinery to diluted bitumen. 1. A unique process for conditioning bitumen so that the bitumen can be processed in an existing light sweet refinery comprising the steps of:providing a blend of a heavy whole bitumen and diluents to produce a diluted bitumen;feeding the blend to a diluent recovery unit (DRU);removing the diluents from the diluted bitumen, in the DRU without additional metallurgy upgrades, to produce a recovered whole bitumen;feeding the recovered whole bitumen to a Resid Hydrocracker;recovering a conditioned whole bitumen having reduced sulfur and nitrogen contents, having eliminated corrosive components, and having a boiling point which is lower than the boiling point of a heavy hydrocarbonaceous feedstock from the Resid Hydrocracker; andfeeding the recovered conditioned lowered boiling point whole bitumen from the Resid Hydrocracker to an integrated atmospheric fractionator.2. The process according to further comprising the steps of:recovering an atmospheric tower bottoms (ATB) product from the atmospheric fractionator; andfeeding the ATB product to a vacuum unit.3. The process according to further comprising the step of:feeding the diluents removed from the diluted bitumen at the DRU to the atmospheric fractionator for further processing to avoid a separate DRU overhead system.4. The process according to further comprising the steps of:recovering an overhead material from the atmospheric fractionator and using the overhead material to preheat the diluted bitumens feeding the DRU.5. The process according to further comprising the step of blending Resid Hydrocracker ATB with conventional ATB for stability control. This invention relates to the optimization of a ...

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Номер записи: 42
23-01-2014 дата публикации

METHOD FOR PRODUCING HYDROCARBON OIL

Номер: US20140021095A1
Автор: Iwama Marie, Tanaka Yuichi, Tasaka Kazuhiko
Принадлежит:

The present invention provides a method for producing a hydrocarbon oil, including performing a hydrocracking by continuously feeding, to a hydrocracking reactor containing a hydrocracking catalyst, a wax to be processed including: a raw wax containing 70% by mass or more of straight-chain hydrocarbons with a boiling point of higher than 360° C.; and an uncracked wax containing 70% by mass or more of straight-chain hydrocarbons with a boiling point of higher than 360° C., which uncracked wax is separated from a hydrocracking product discharged from the reactor, to thereby yield a hydrocarbon oil including hydrocarbons with a boiling point of 360° C. or lower. 1. A method for producing a hydrocarbon oil , comprising performing a hydrocracking by continuously feeding , to a hydrocracking reactor containing a hydrocracking catalyst , a wax to be processed comprising: a raw wax containing 70% by mass or more of straight-chain hydrocarbons with a boiling point of higher than 360° C.; and an uncracked wax containing 70% by mass or more of straight-chain hydrocarbons with a boiling point of higher than 360° C. , which uncracked wax is separated from a hydrocracking product discharged from the reactor , to thereby yield a hydrocarbon oil comprising hydrocarbons with a boiling point of 360° C. or lower , wherein{'sub': 1', '2, 'claim-text': [{'br': None, 'Cracking rate (%)=((content of hydrocarbons with boiling point of higher than 360° C. in 1 g of wax to be processed)−(content of hydrocarbons with boiling point of higher than 360° C. in 1 g of hydrocracking product))×100/(content of hydrocarbons with boiling point of higher than 360° C. in 1 g of wax to be processed)\u2003\u2003(1);'}, {'br': None, 'i': '≦X', 'sub': '1', '30≦90\u2003\u2003(2); and'}, {'br': None, 'i': ≦X', '/X, 'sub': 2', '1, '0.1≦0.9\u2003\u2003(3).'}], 'the following periods are alternately provided: a period for performing hydrocracking of the wax to be processed under a condition where a cracking rate ...

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Номер записи: 43
30-01-2014 дата публикации

Dual stripper column apparatus and methods of operation

Номер: US20140027347A1
Автор: Richard K. Hoehn, Vedula K. Murty
Принадлежит: UOP LLC

Dual stripper column arrangements are described in which hot flash drum liquid is sent to one column and cold flash drum liquid is sent to a second column. Methods of operating the dual stripper column apparatus are also described.

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Номер записи: 44
30-01-2014 дата публикации

PROCESS FOR HYDROTREATING HEAVY HYDROCARBON FEEDS WITH SWITCHABLE REACTORS INCLUDING AT LEAST ONE STEP OF PROGRESSIVE SWITCHING

Номер: US20140027351A1
Автор: BAZER-BACHI Frederic, Digne Mathieu, Marchal Nicolas, Plain Cecile, Verstraete Jan
Принадлежит: IFP ENERGIES NOUVELLES

Process for hydrotreating a heavy hydrocarbon fraction using a system of switchable fixed bed guard zones each containing at least one catalyst bed including at least one step during which the flow of feed supplied to the first guard zone brought into contact with the feed is partly displaced to the next guard zone downstream, preferably progressively. 1. Process for hydrotreating a heavy hydrocarbon fraction containing asphaltenes , sediments , sulphur-containing , nitrogen-containing and metallic impurities , in which the feed of hydrocarbons and hydrogen is passed , under hydrotreating conditions , over a hydrotreating catalyst , in at least two fixed bed hydrotreating guard zones each containing at least one catalyst bed , the guard zones being arranged in series to be used cyclically , consisting of successive repetition of steps b) , c) and c′) defined below:a step a) during which the feed passes through all the guard zones during a fraction of the deactivation time and/or clogging time of the first guard zone brought into contact with the feed,a step a′) during which a portion of the feed continues to pass through the first guard zone brought into contact with the feed and another portion of the feed is introduced into the next guard zone downstream for a period at most equal to the deactivation time and/or clogging time of the first guard zone brought into contact with the feed,a step b) during which the deactivated and/or clogged guard zone is by-passed and the catalyst that it contains is regenerated and/or replaced with fresh catalyst and during which the other guard zone(s) are used,a step c) during which the feed passes through all the guard zones, the guard zone of which the catalyst was regenerated during the preceding step being reconnected so as to be downstream of all the other guard zones and said step being continued for a fraction of the deactivation time and/or clogging time of the first guard zone brought into contact with the feed,a step c′) ...

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Номер записи: 45
13-02-2014 дата публикации

Process for passivation by a nitrogen-containing compound of a zeolitic catalyst, in particular a hydrocracking catalyst

Номер: US20140042057A1
Автор: Mickael Bremaud, Pauline Galliou, Pierre Dufresne, Sharath Kirumakki
Принадлежит: Europeene de Retraitement de Catalysateurs EURECAT

The invention relates to a process for ex-situ treatment of a catalyst that contains at least one hydrogenating phase, and at least one amorphous silica-alumina or a zeolite that contains acid sites, whereby said process comprises: A stage for introducing nitrogen by contact at a temperature that is less than 100° C., with at least one basic nitrogen-containing compound that is ammonia or a compound that can be decomposed into ammonia, with said compound being introduced at a rate of 0.5-10% by weight (expressed in terms of N), and A sulfurization/activation stage with a gas that contains hydrogen and hydrogen sulfide at a temperature of at least 250° C., with this stage being carried out before or after the stage for introducing said nitrogen-containing compound, and the catalyst that is obtained is optionally dried. This treatment allows a rapid, effective start-up on the hydrocracking unit.

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Номер записи: 46
27-02-2014 дата публикации

Hydrovisbreaking Process for Feedstock Containing Dissolved Hydrogen

Номер: US20140054199A1
Автор: Omer Refa Koseoglu
Принадлежит: Saudi Arabian Oil Co

An improved hydrovisbreaking process for reducing the viscosity of a liquid hydrocarbon feedstock is provided. A substantially single-phase hydrogen-enriched liquid hydrocarbon feedstock is obtained by mixing the feedstock with hydrogen gas and flashing off the excess hydrogen gas. Comparatively smaller reactor vessels can be used without a gas recycle system, thus reducing the capital cost of hydrovisbreaking process. Further the need for cutter stocks can be minimized or eliminated.

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Номер записи: 47
06-03-2014 дата публикации

UZM-39 ALUMINOSILICATE ZEOLITE

Номер: US20140066674A1
Автор: Miller Mark A., Nicholas Christopher P.
Принадлежит: UOP LLC

A new family of coherently grown composites of TUN and IMF zeotypes have been synthesized. These zeolites are represented by the empirical formula. 2. The process of wherein the hydrocarbon conversion process is selected from the group consisting of cracking claim 1 , hydrocracking claim 1 , alkylation of aromatics or isoparaffins claim 1 , isomerization of paraffin claim 1 , olefins claim 1 , or poly-alkylbenzene such as xylene claim 1 , trans-alkylation of poly-alkybenzene with benzene or mono-alkybenzene claim 1 , disproportionation of mono-alkybenzene claim 1 , polymerization claim 1 , reforming claim 1 , hydrogenation claim 1 , dehydrogenation claim 1 , transalkylation claim 1 , dealkylation claim 1 , hydration claim 1 , dehydration claim 1 , hydrotreating claim 1 , hydrodenitrogenation claim 1 , hydrodesulfurization claim 1 , methanation claim 1 , syngas shift process and combinations thereof.3. The process of further comprising removing an effluent comprising the at least one converted product claim 1 , fractionating the effluent claim 1 , and recovering at least one converted product.4. The process of further comprising claim 3 , subjecting the effluent to partial condensation and vapor-liquid separation prior to fractionation.5. The process of further comprising recycling at least a portion of the effluent to the catalyst.7. The process of wherein the hydrocarbon conversion process is selected from the group consisting of cracking claim 6 , hydrocracking claim 6 , alkylation of aromatics or isoparaffins claim 6 , isomerization of paraffin claim 6 , olefins claim 6 , or poly-alkylbenzene such as xylene claim 6 , trans-alkylation of poly-alkybenzene with benzene or mono-alkybenzene claim 6 , disproportionation of mono-alkybenzene claim 6 , polymerization claim 6 , reforming claim 6 , hydrogenation claim 6 , dehydrogenation claim 6 , transalkylation claim 6 , dealkylation claim 6 , hydration claim 6 , dehydration claim 6 , hydrotreating claim 6 , ...

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Номер записи: 48
20-03-2014 дата публикации

CATALYST FOR USE IN HYDROTREATMENT, COMPRISING METALS FROM GROUPS VIII AND VIB, AND PREPARATION WITH CITRIC ACID AND C1-C4 DIALKYL SUCCINATE

Номер: US20140076780A1
Автор: Dath Jean-Pierre, DE GRANDI Valentina, GUICHARD Bertrand, Minoux Delphine, SIMON Laurent
Принадлежит:

A catalyst which comprises an amorphous support based on alumina, a C1-C4 dialkyl succinate, citric acid and optionally acetic acid, phosphorus and a hydrodehydrogenating function comprising at least one element from group VIII and at least one element from group VIB; the most intense bands comprised in the Raman spectrum of the catalyst are characteristic of Keggin heteropolyanions (974 and/or 990 cm), C1-C4 dialkyl succinate and citric acid (in particular 785 and 956 cm). Also a process for preparing said catalyst in which a catalytic precursor in the dried, calcined or regenerated state containing the elements of the hydrodehydrogenating function, and optionally phosphorus, is impregnated with an impregnation solution comprising at least one C1-C4 dialkyl succinate, citric acid and optionally at least one compound of phosphorus and optionally acetic acid, and is then dried. Further, the use of said catalyst in any hydrotreatment process. 1. A catalyst comprising an amorphous support based on alumina , at least one C1-C4 dialkyl succinate , citric acid , phosphorus and a hydrodehydrogenating function comprising at least one element from group VIB and at least one element from group VIII , with the Raman spectrum of the catalyst comprising bands at 990 and/or 974 cm , characteristic of at least one Keggin heteropolyanion , the characteristic bands of said succinate and the principal characteristic bands of citric acid.2. A catalyst according to claim 1 , in which the dialkyl succinate is dimethyl succinate and in which the Raman spectrum of the catalyst has principal bands at 990 and/or 974 cmcharacteristic of Keggin heteropolyanions claim 1 , and at 853 cm claim 1 , characteristic of dimethyl succinate and at 785 and 956 cm claim 1 , characteristic of citric acid.3. A catalyst according to claim 1 , also comprising acetic acid the Raman spectrum of which includes a line at 896 cm claim 1 , characteristic of acetic acid.4. A catalyst according to claim 1 , in which ...

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Номер записи: 49
20-03-2014 дата публикации

REGENERATED HYDROGENATION REFINING CATALYST AND METHOD FOR PRODUCING A HYDROCARBON OIL

Номер: US20140076782A1
Автор: Iwama Marie, Niitsuma Takuya, Tanaka Yuichi, Tasaka Kazuhiko
Принадлежит:

The regenerated hydrotreating catalyst of the present invention is a regenerated hydrotreating catalyst prepared by regenerating a used hydrotreating catalyst comprising a catalyst support including an amorphous composite metal oxide having solid acidity, and at least one active metal supported by the catalyst support and selected from noble metals of Group 8 to Group 10 in the periodic table, wherein the regenerated hydrotreating catalyst contains 0.05 to 1% by mass of a carbonaceous substance in terms of a carbon atom based on the entire mass of the catalyst. 1. A regenerated hydrotreating catalyst prepared by regenerating a used hydrotreating catalyst comprising a catalyst support comprising an amorphous composite metal oxide having solid acidity , and at least one active metal supported by the catalyst support and selected from noble metals of Group 8 to Group 10 in the periodic table , whereinthe regenerated hydrotreating catalyst contains 0.05 to 1% by mass of a carbonaceous substance in terms of a carbon atom based on the entire mass of the catalyst.2. The regenerated hydrotreating catalyst according to claim 1 , wherein the amorphous composite metal oxide is at least one selected from silica zirconia claim 1 , silica alumina claim 1 , and alumina boria.3. The regenerated hydrotreating catalyst according to claim 1 , wherein the active metal is platinum.4. A process for producing a hydrocarbon oil claim 1 , comprising contacting a raw oil comprising 80% by mass or more of straight-chain aliphatic hydrocarbons whose boiling point is in the range of 25 to 360° C. and comprising 20% by mass or more of straight-chain aliphatic hydrocarbons whose boiling point is in the range of 150 to 360° C. claim 1 , with a regenerated hydrotreating catalyst according to in the presence of molecular hydrogen.5. The process for producing a hydrocarbon oil according to claim 4 , wherein the raw oil is a synthetic oil obtained by a Fischer-Tropsch synthesis reaction.6. The ...

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Номер записи: 50
20-03-2014 дата публикации

INTERSTITIAL METAL HYDRIDE CATALYST SYSTEMS AND ASSOCIATED PROCESSES

Номер: US20140081060A1
Автор: Bai Chuansheng, Beeckman Jean W., Borghard William G., Elsen Heather A., Thornburg Adrienne J.
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Exemplary embodiments of the present invention relate to the processing of hydrocarbon-containing feedstreams in the presence of an interstitial metal hydride containing catalyst comprising a surface, and a Group VI/Group VIII metal sulfide coated onto the surface of the interstitial metal hydride. The catalysts and processes of the present invention can improve overall hydrogenation, product conversion, as well as sulfur reduction in hydrocarbon feedstreams. 1. A process for upgrading a hydrocarbon feedstream , comprising contacting a hydrocarbon feedstream with a catalyst comprising an interstitial metal hydride having a surface and a Group VI/Group VIII metal sulfide coated on the surface of the interstitial metal hydride , in the presence of hydrogen to yield an upgraded hydrocarbon product stream.2. The process of claim 1 , wherein process is performed in the presence of a hydrogen-rich gas containing at least 50 mol % hydrogen.3. The process of claim 1 , wherein the hydrocarbon feedstream is a heavy hydrocarbon feedstream with an API gravity of less than 20 and a sulfur content of at least 1 wt % sulfur.4. The process of claim 1 , wherein the hydrocarbon feedstream comprises a biofuel.5. The process of claim 1 , wherein the process is a hydroprocessing process selected from hydrogenation claim 1 , hydrocracking claim 1 , hydrodesulfurization claim 1 , hydrodenitrogenation claim 1 , hydrodemetalization claim 1 , and catalytic hydrodewaxing processes.6. The process of claim 1 , wherein the Group VI metal is selected from Mo and W; the Group VIII metal is selected from Fe claim 1 , Co claim 1 , Ni claim 1 , Pd claim 1 , and Pt; and wherein the interstitial metal hydride and the Group VI/Group VIII metal sulfide are present in a ratio of about 20:80 by weight to about 80:20 by weight. This application is a divisional application of U.S. patent application Ser. No. 12/942,271, filed on Nov. 9, 2010.The present invention relates to catalysts for the processing of ...

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Номер записи: 51
27-03-2014 дата публикации

REGENERATED HYDROCRACKING CATALYST AND METHOD FOR PRODUCING A HYDROCARBON OIL

Номер: US20140083907A1
Автор: Iwama Marie, Niitsuma Takuya, Tanaka Yuichi, Tasaka Kazuhiko
Принадлежит:

The regenerated hydrocracking catalyst according to the present invention is a regenerated hydrocracking catalyst prepared by regenerating a used hydrocracking catalyst including: a catalyst support containing zeolite and an amorphous composite metal oxide having solid acidity; and at least one active metal supported by the catalyst support, selected from noble metals of Group 8 to Group 10 in the periodic table, wherein the regenerated hydrocracking catalyst contains 0.05 to 1% by mass of a carbonaceous substance in terms of carbon atoms based on the entire mass of the catalyst. 1. A regenerated hydrocracking catalyst prepared by regenerating a used hydrocracking catalyst comprising: a catalyst support containing zeolite and an amorphous composite metal oxide having solid acidity; and at least one active metal supported by the catalyst support , selected from noble metals of Group 8 to Group 10 in the periodic table , wherein the regenerated hydrocracking catalyst contains 0.05 to 1% by mass of a carbonaceous substance in terms of carbon atoms based on the entire mass of the catalyst.2. The regenerated hydrocracking catalyst according to claim 1 , wherein the zeolite is an ultra stable Y zeolite.3. The regenerated hydrocracking catalyst according to wherein the amorphous composite metal oxide is at least one selected from silica alumina claim 1 , alumina boria claim 1 , and silica zirconia.4. The regenerated hydrocracking catalyst according to claim 1 , wherein the active metal is platinum.5. A process for producing a hydrocarbon oil claim 1 , comprising contacting a raw material oil containing 70% by mass or more of a linear aliphatic hydrocarbon with a boiling point of higher than 360° C. with the hydrocracking catalyst according to in the presence of molecular hydrogen.6. The process for producing a hydrocarbon oil according to claim 5 , wherein the raw material oil is a synthetic oil obtained by a Fischer-Tropsch synthesis reaction.7. The regenerated ...

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Номер записи: 52
10-04-2014 дата публикации

INTEGRATED HYDROPROCESSING

Номер: US20140097123A1
Автор: ARMISTEAD George, MAY Simon, STANLEY Bill
Принадлежит:

The present invention relates to a method and system for converting gas to liquids and fractionating crude oil or condensate. Advantageously, it includes hydroprocessing at least a portion of the fractionated product and at least a portion of the Fischer-Tropsch products in the same hydroprocessor. Among other advantages the present invention provides for improved output quality for diesel and/or naphtha, reduced transportation and/or storage costs, and/or enhanced energy efficiency. 1. A process comprising:fractionating crude oil, condensate, or a mixture thereof in a fractionator to produce a fractionated product comprising diesel, kerosene, or a mixture thereof;employing synthesis gas in a Fischer-Tropsch reactor to produce one or more Fischer-Tropsch products; andhydroprocessing at least a portion of the fractionated product and at least a portion of the Fischer-Tropsch products in the same hydroprocessor.2. The process of which further comprises generating heat in the Fischer-Tropsch reaction and transferring at least a portion of said heat to the fractionator.3. The process of which further comprises converting natural gas to synthesis gas wherein at least a portion of said synthesis gas is employed in the Fischer-Tropsch reaction.4. The process of wherein said hydroprocessing comprises hydrogenating claim 1 , hydrocracking claim 1 , hydroisomerization claim 1 , or hydrotreating.5. The process of wherein the synthesis gas is produced from an autothermal reformer claim 1 , a steam methane reformer claim 1 , or a partial oxidation reformer.6. The process of wherein the hydroprocessing produces naphtha claim 1 , diesel claim 1 , gas oils claim 1 , LPG claim 1 , kerosene claim 1 , jet fuel claim 1 , or a mixture thereof.7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. The process of wherein said hydroprocessing comprises hydrogenating.13. The process of wherein said hydroprocessing comprises hydrocracking.14. The process of wherein said ...

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Номер записи: 53
10-04-2014 дата публикации

Addition of a Modified Vapor Line Reactor Process to a Coking Process

Номер: US20140097124A1
Автор: ETTER Roger G.
Принадлежит:

A reactor process added to a coking process to modify the quantity or yield of a coking process product and/or modify certain characteristics or properties of coking process products. 1. A process comprising adding a reactor process to a coking process wherein said addition of a reactor process comprises the addition of a reactor vessel , the modification of the traditional vapor line between the coke drum and the fractionator to perform as a reactor vessel , or any combination thereof and associated equipment to promote chemical reactions of a process stream from said coking process and return products of said reactor process to said coking process to cause a modification of a quantity , a yield characteristic , a quality , or a property of a product resulting from said coking process.2. A process of wherein said reactor process is selected from the group consisting of riser cracking reactor claim 1 , fluidized bed reactor claim 1 , ebullated bed reactor claim 1 , fixed bed reactor claim 1 , bunker reactor claim 1 , plug flow reactor claim 1 , or other reactor processes.3. A process of wherein said coking process is selected from the group consisting of delayed coking claim 1 , fluid coking claim 1 , flexicoking claim 1 , or other coking processes.4. A process of wherein said modification is caused by the introduction of an additive to said reactor process claim 1 , said additive comprising catalyst(s) claim 1 , seeding agent(s) claim 1 , excess reactant(s) claim 1 , quenching agent(s) claim 1 , carrier fluid(s) claim 1 , or any combination thereof.5. A process of wherein said catalyst is an acid based catalyst that provides propagation of carbon based free radicals that actively participate in a mechanism of a cracking reaction claim 4 , a coking reaction claim 4 , or any combination thereof6. A process of wherein said catalyst is selected from the group consisting of alumina claim 4 , silica claim 4 , zeolite claim 4 , calcium compounds claim 4 , iron compounds ...

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Номер записи: 54
02-01-2020 дата публикации

POORLY CRYSTALLINE TRANSITION METAL TUNGSTATE

Номер: US20200001281A1
Автор: Koster Susan C., Miller Stuart R.
Принадлежит:

A hydroprocessing catalyst has been developed. The catalyst is a poorly crystalline transition metal tungstate material or a metal sulfide decomposition product thereof. The hydroprocessing using the crystalline ammonia transition metal tungstate material may include hydrodenitrification, hydrodesulfurization, hydrodemetallation, hydrodesilication, hydrodearomatization, hydroisomerization, hydrotreating, hydrofining, and hydrocracking. 2. The poorly crystalline transition metal tungstate material of wherein the poorly crystalline transition metal tungstate material is present in a mixture with at least one binder and wherein the mixture comprises up to 25 wt-% binder.3. The poorly crystalline transition metal tungstate material of wherein the binder is selected from the group consisting of silicas claim 2 , aluminas claim 2 , and silica-aluminas.4. The poorly crystalline transition metal tungstate material of wherein M is nickel or zinc.5. The poorly crystalline transition metal tungstate material of wherein M is nickel.7. The method of further comprising removing at least some of the NH claim 6 , HO or combination thereof to form an intermediate before reacting the mixture at a temperature from about 90° C. to about 350° C. in an autogenous environment.8. The method of wherein the reacting is conducted from about 30 minutes to 14 days.9. The method of wherein the recovering is by filtration or centrifugation.10. The method of further comprising adding a binder to the poorly crystalline transition metal tungstate material.11. The method of wherein the binder is selected from the group consisting of aluminas claim 10 , silicas claim 10 , and alumina-silicas.12. The method of further comprising decomposing the poorly crystalline transition metal tungstate material by sulfidation to form metal sulfides.14. The process of wherein the conversion process is hydroprocessing.15. The process of wherein the conversion process is selected from the group consisting of ...

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Номер записи: 55
03-01-2019 дата публикации

MOLECULAR SIEVE SSZ-95, METHOD OF MAKING, AND USE

Номер: US20190001312A1
Автор: Lei Guan-Dao, Ojo Adeola Florence, Zhang Yihua, Zones Stacey Ian
Принадлежит: Chevron U.S.A. INC.

A new crystalline molecular sieve designated SSZ-95 is disclosed. In general, SSZ-95 is synthesized from a reaction mixture suitable for synthesizing MTT-type molecular sieves and maintaining the mixture under crystallization conditions sufficient to form product. The product molecular sieve is subjected to a pre-calcination step, and ion-exchange to remove extra-framework cations, and a post-calcination step. The molecular sieve has a MTT-type framework and a H-D exchangeable acid site density of 0 to 50% relative to molecular sieve SSZ-32. 1. A molecular sieve having a MTT-type framework , a mole ratio of 20 to 70 of silicon oxide to aluminum oxide , a total micropore volume of between 0.005 and 0.02 cc/g; and a H-D exchangeable acid site density of up to 50% relative to SSZ-32.2. The molecular sieve of claim 1 , wherein the molecular sieve has a mole ratio of 20 to 50 of silicon oxide to aluminum oxide.3. The molecular sieve of claim 1 , wherein the molecular sieve has a total micropore volume of between 0.008 and 0.018 cc/g.4. The molecular sieve of claim 1 , wherein the molecular sieve has an external surface area of between 200 and 250 m/g; and a BET surface area of between 240 and 280 m/g.5. The molecular sieve of claim 1 , wherein the molecular sieve has a H-D exchangeable acid site density of 0.5 to 30% relative to molecular sieve SSZ-32.6. The molecular sieve of claim 5 , wherein the molecular sieve has a total micropore volume of between 0.008 and 0.018 cc/g.7. The molecular sieve of claim 5 , wherein the molecular sieve has an external surface area of between 200 and 250 m/g; and a BET surface area of between 240 and 280 m/g.8. The molecular sieve of claim 1 , wherein the molecular sieve has a H-D exchangeable acid site density of 2 to 25% relative to molecular sieve SSZ-32.9. The molecular sieve of claim 8 , wherein the molecular sieve has a total micropore volume of between 0.008 and 0.018 cc/g.10. The molecular sieve of claim 8 , wherein the molecular ...

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Номер записи: 56
05-01-2017 дата публикации

CIT-10: A TWO DIMENSIONAL LAYERED CRYSTALLINE MICROPOROUS SILICATE COMPOSITION AND COMPOSITIONS DERIVED THEREFROM

Номер: US20170001872A1
Автор: Davis Mark E., SCHMIDT JOEL E.
Принадлежит:

This disclosure relates to a new crystalline microporous silicate solid, designated CIT-10, comprising a two dimensional layered structure, having an organic interlayer sandwiched between individual crystalline silicate layers. This CIT-10 material can be converted to a pure-silicate of RTH topology, as well as two new of pillared silicate structures, designated CIT-11 and CIT-12. This disclosure characterizes new materials and provides methods of preparing and using these new crystalline microporous solids. 1. A crystalline microporous silicate , designated CIT-10 , which exhibits a powder X-ray diffraction (XRD) pattern exhibiting at least five of the characteristic peaks at 7.6±0.2° , 8.7±0.2° , 10.3±0.2° , 18.8±0.2° , 20.3±0.2° , 21.8±0.2° , 22.4±0.2° , 22.7±0.2° , 22.9±0.2° , and 23.6±0.2° 2-theta.2. The crystalline microporous silicate of claim 1 , wherein the crystalline microporous silicate comprises a two dimensional layered structure claim 1 , having an organic material sandwiched between individual crystalline silicate layers.3. The crystalline microporous silicate of claim 2 , having a structure which is ordered along its two dimensional crystalline silicate layers claim 2 , but which exhibits disorder between its crystalline silicate layers claim 2 , as evidenced by RED (rotating electron diffraction) structure analysis.4. The crystalline microporous silicate of claim 1 , which exhibits an Si-MAS NMR spectrum having resonances at chemical shifts of −113 ppm claim 1 , −107 ppm claim 1 , and −102 ppm claim 1 , relative to tetramethylsilane (TMS).5. The crystalline microporous silicate of claim 4 , wherein the resonances at chemical shifts of −113 ppm claim 4 , −107 ppm claim 4 , and −102 ppm have relative integrated intensities of 8 claim 4 , 5 claim 4 , and 3 claim 4 , respectively.7. A crystalline microporous silicate claim 4 , designated CIT-11 claim 4 , which exhibits a powder X-ray diffraction (XRD) pattern exhibiting at least five of the ...

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Номер записи: 57
07-01-2016 дата публикации

COMMERCIAL FISCHER-TROPSCH REACTOR

Номер: US20160002541A1
Автор: BOHN MARK, HOGSETT FRANK, IBSEN Mark, MOHEDAS SERGIO, WRIGHT Harold A.
Принадлежит:

A method for converting synthesis gas into liquid hydrocarbons by introducing a synthesis gas feed into a Fischer-Tropsch system that includes a catalytic reactor fluidly connected with at least two slurry loops, the reactor comprising at least as many reactor product outlets and slurry return inlets as slurry loops; each slurry loop comprising a separation system comprising at least one separator, an inlet of each separator fluidly connected to a reactor product outlet via a slurry offtake, and an outlet of each separator fluidly connected to a slurry return inlet via a slurry return; separating concentrated catalyst slurry from the reaction product via the slurry loops; removing liquid hydrocarbon product from each separator; and returning concentrated catalyst slurry to the catalytic reactor via the slurry returns and slurry return inlets. A system for converting synthesis gas into liquid hydrocarbons via the method is also disclosed. 1. A method for converting synthesis gas into liquid hydrocarbons , the method comprising:introducing a synthesis gas feed into a Fischer-Tropsch reactor of a Fischer-Tropsch system at a superficial gas velocity greater than the average sedimentation velocity and/or greater than the minimum fluidization velocity of catalyst in the catalytic reactor, wherein the Fischer-Tropsch system comprises: a catalytic reactor fluidly connected with at least two slurry loops, wherein the reactor comprises at least as many reactor product outlets and at least as many slurry return inlets as slurry loops; wherein each slurry loop comprises a separation system comprising at least one separator for separating concentrated catalyst slurry from liquid product; an inlet of the at least one separator fluidly connected to one of the reactor product outlets via a slurry offtake, an outlet of the at least one separator fluidly connected to one of the slurry return inlets via a slurry return, and a product outlet of the at least one separator for removal of ...

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Номер записи: 58
05-01-2017 дата публикации

FUEL PRODUCTION FROM FCC PROCESSING

Номер: US20170002279A1
Автор: Barrai Federico, Brown Stephen H., CUNNINGHAM Brian A., Kar Kenneth C.H., Rubin-Pitel Sheryl B.
Принадлежит:

Systems and methods are provided for upgrading catalytic slurry oil to form naphtha boiling range and/or distillate boiling range fuel products. It has been unexpectedly discovered that catalytic slurry oil can be separately hydroprocessed under fixed bed conditions to achieve substantial conversion of asphaltenes within the slurry oil (such as substantially complete conversion) while reducing/minimizing the amount of coke formation on the hydroprocessing catalyst. After hydroprocessing, the hydroprocessed effluent can be processed under fluid catalytic cracking conditions to form various products, including distillate boiling range fuels and/or naphtha boiling range fuels. Another portion of the effluent can be suitable for use as a low sulfur fuel oil, such as a fuel oil having a sulfur content of 0.1 wt % or less. 1. A method for processing a product fraction from a fluid catalytic cracking (FCC) process , comprising:exposing a feed composed substantially of an FCC product fraction including a ˜650° F.+ (˜343° C.+) portion to a hydrotreating catalyst in a fixed bed under effective hydrotreating conditions to form a hydrotreated effluent, the ˜343° C.+ portion of the FCC product fraction comprising a density of at least about 1.06 g/cc, the ˜343° C.+ portion comprising at least about 2 wt % n-heptane insolubles, at least a first amount of micro carbon residue, or a combination thereof,{'sub': 3', '3, 'wherein a C+ portion of the hydrotreated effluent comprises a density of about 1.02 g/cc or less, the C+ portion of the hydrotreated effluent comprising less than about 1 wt % n-heptane insolubles, less than about half of the first amount of micro carbon residue, or a combination thereof.'}2. The method of claim 1 , wherein the FCC product fraction includes about 3 wt % to about 10 wt % of a ˜1050° F.+ (˜566° C.+) portion claim 1 , the effective hydrotreating conditions being effective for conversion of at least about 60 wt % of the ˜566° C.+ portion of the FCC ...

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Номер записи: 59
04-01-2018 дата публикации

PROCESSING OF HEAVY HYDROCARBON FEEDS

Номер: US20180002617A1
Автор: Bai Chuansheng, Brown Stephen H., Cheng Jane C., Dankworth David C., Degnan, Dougherty Richard C., Falkiner Robert J., Gupta Himanshu, Harandi Mohsen N., Henao Juan D., HUGHART Cindy J., JR. Thomas F., Levine Steven W., Marut Todd P., NELSON John D., Soled Stuart L., Umansky Benjamin S., ZHANG LEI
Принадлежит:

Systems and methods are provided for hydroconversion of a heavy oil feed under slurry hydroprocessing conditions and/or solvent assisted hydroprocessing conditions. The systems and methods for slurry hydroconversion can include the use of a configuration that can allow for improved separation of catalyst particles from the slurry hydroprocessing effluent. In addition to allowing for improved catalyst recycle, an amount of fines in the slurry hydroconversion effluent can be reduced or minimized. This can facilitate further processing or handling of any “pitch” generated during the slurry hydroconversion. The systems and methods for solvent assisted hydroprocessing can include processing of a heavy oil feed in conjunction with a high solvency dispersive power crude. 1. A process for producing a hydroprocessed product , comprising:exposing a feedstock to a catalyst under effective slurry hydroconversion conditions to form a slurry hydroprocessing effluent, the effective slurry hydroconversion conditions being effective for conversion of at least about 90 wt % of the feedstock relative to a conversion temperature, the catalyst comprising catalyst particles having a particle size of at least about 2 μm; andseparating at least about 95 wt % of the catalyst particles having a particle size of at least about 2 μm from the slurry hydroprocessing effluent using a catalyst recovery system comprising one or more drum separators and a cross-flow filter.2. The process of claim 1 , wherein the feedstock has a T95 distillation point of about 600° C. or less.3. The process of claim 1 , wherein the feedstock has a 10% distillation point of at least about 900° F. (˜482° C.) claim 1 , a Conradson carbon residue of at least about 27.5 wt % claim 1 , or a combination thereof.4. The process of claim 1 , wherein the one or more drum separators comprise cyclone separators.5. The process of claim 1 , further comprising exposing the feedstock to a demetallization catalyst under slurry ...

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Номер записи: 60
02-01-2020 дата публикации

Supercritical Water Separation Process

Номер: US20200002629A1
Автор: Coppola Edward N., JR. Charles, Nana Sanjay, Pelt Kenneth D., Red, Wahlgren Jocelyn Marie
Принадлежит:

A supercritical water separation process and system is disclosed for the removal of metals, minerals, particulate, asphaltenes, and resins from a contaminated organic material. The present invention takes advantage of the physical and chemical properties of supercritical water to effect the desired separation of contaminants from organic materials and permit scale-up. At a temperature and pressure above the critical point of water (374° C., 22.1 MPa), nonpolar organic compounds become miscible in supercritical water (SCW) and polar compounds and asphaltenes become immiscible. The process and system disclosed continuously separates immiscible contaminants and solids from the supercritical water and clean oil product solution. The present invention creates a density gradient that enables over 95% recovery of clean oil and over 99% reduction of contaminants such as asphaltenes and particulate matter depending on the properties of the contaminated organic material. 1. A process for treating a feedstock comprising:delivering a feedstock and supercritical water into a hydrothermal separation vessel, said hydrothermal separation vessel including an upper separation zone, a mid-level mixing zone, and a bottom concentration zone, wherein the feedstock and supercritical water are fed separately into the mixing zone to form a mixture, said mixing zone providing sufficient shear and mixing to cause dissolution of any soluble components of the feedstock into the supercritical water;maintaining a temperature and pressure within the hydrothermal separation vessel to achieve a vertical density gradient therein such that the separation zone exhibits a lower density than the concentration zone to form a product stream and a stream containing insoluble components; andremoving the product stream from the separation zone and the stream containing insoluble components from the concentration zone.2. The process of claim 1 , wherein any components present in the feedstock that are ...

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Номер записи: 61
07-01-2021 дата публикации

CATALYST PRECURSOR FOR HYDROCRACKING REACTION AND METHOD FOR HYDROCRACKING HEAVY OIL BY USING SAME

Номер: US20210002563A1
Автор: CHOI Byong Min, CHUNG Minchul, Kim Gyoo Tae, LEE Chul Wee, PARK Sunyoung, SEO Hwi Min, SON Seok Hwan
Принадлежит:

The present invention relates to a catalyst precursor for forming a molybdenum disulfide catalyst through a reaction with sulfur in heavy oil and to a method for hydrocracking heavy oil by using same. According to the present invention, the yield of a low-boiling liquid product with a high economic value in the products by heavy oil cracking can be increased, and the yield of a relatively uneconomical gas product or coke (toluene insoluble component), which is a byproduct, can be significantly lowered. 1. A catalyst precursor for a hydrocracking reaction represented by the following Chemical Formula 1 or Chemical Formula 2 , which reacts with sulfur in a heavy oil to produce a molybdenum disulfide catalyst:{'br': None, 'sub': 2', '2', '2, 'Mo(O)(O)L\u2003\u2003[Chemical Formula 1]'}{'br': None, 'sub': 4', '2, 'Mo(CO)L′\u2003\u2003[Chemical Formula 2]'}whereinL and L′ are a ligand having a coordination number of 1, containing phosphorus as a central element.3. The catalyst precursor for a hydrocracking reaction of claim 2 , wherein Rto Rof Chemical Formula 3 are independently of one another hydroxy claim 2 , C-Calkoxy claim 2 , C-Ccycloalkyloxy claim 2 , or C-Caryloxy.4. The catalyst precursor for a hydrocracking reaction of claim 2 , wherein Rto Rof Chemical Formula 3 are independently of one another C-Calkyl claim 2 , C-Ccycloalkyl claim 2 , C-Ccycloalkyl C-Calkyl claim 2 , or C-Calkyl C-Ccycloalkyl.5. The catalyst precursor for a hydrocracking reaction of claim 2 , wherein Rto Rof Chemical Formula 3 are independently of one another C-Caryl claim 2 , C-Caryl C-Calkyl claim 2 , or C-Calkyl C-Caryl.7. The catalyst precursor for a hydrocracking reaction of claim 6 , wherein Rto Rof Chemical Formula 4 are independently of one another C-Calkyl claim 6 , C-Ccycloalkyl claim 6 , C-Ccycloalkyl C-Calkyl claim 6 , or C-Calkyl C-Ccycloalkyl.8. The catalyst precursor for a hydrocracking reaction of claim 1 , wherein the molybdenum disulfide catalyst is a molybdenum disulfide ...

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Номер записи: 62
13-01-2022 дата публикации

METHODS OF PRODUCING HYDROCRACKING CATALYST

Номер: US20220008908A1
Автор: Hodgkins Robert Peter, KOSEOGLU Omer Refa, Uchida Koji, Watabe Mitsunori
Принадлежит:

A method for producing a hydrocracking catalyst includes preparing a framework substituted Y-type zeolite, preparing a binder, co-mulling the framework substituted Y-type zeolite, the binder, and one or more hydrogenative metal components to form a catalyst precursor, and calcining the catalyst precursor to generate the hydrocracking catalyst. The framework substituted Y-type zeolite is prepared by calcining a Y-type zeolite at 500° C. to 700° C. to form a calcined Y-type zeolite. Further, the framework substituted Y-type zeolite is prepared by forming a suspension containing the calcined Y-type zeolite, the suspension having a liquid to solid mass ratio of 5 to 15, adding acid to adjust the pH of the suspension to less than 2.0, adding and mixing one or more of a zirconium compound, a hafnium compound, or a titanium compound to the suspension, and neutralizing the pH of the suspension to obtain the framework substituted Y-type zeolite. 1. A method for producing a hydrocracking catalyst , the method comprising: [{'sup': '2', 'sub': 2', '2', '3, 'calcining a Y-type zeolite at 500° C. to 700° C. to form a calcined Y-type zeolite, the Y-type zeolite having a crystal lattice constant failing in an inclusive range of 2.430 to 2.450 nm, a specific surface area of 600 to 900 m/g, and a molar ratio of SiOto AlOof 20 to 100;'}, 'forming a suspension containing the calcined Y-type zeolite, the suspension having a liquid to solid mass ratio of 5 to 15;', 'adding acid to adjust the pH of the suspension to less than 2.0;', 'adding and mixing one or more of a zirconium compound, a hafnium compound, or a titanium compound to the suspension; and', 'neutralizing the pH of the suspension to obtain the framework substituted Y-type zeolite;, 'preparing a framework substituted Y-type zeolite, wherein the framework substituted Y-type zeolite is prepared bypreparing a binder;co-mulling the framework substituted Y-type zeolite, the binder, and one or more hydrogenative metal components to ...

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Номер записи: 63
27-01-2022 дата публикации

METHODS OF CO-PROCESSING PETROLEUM DISTILLATES AND BIO-BASED MATERIAL THROUGH A REACTION SERIES

Номер: US20220025279A1
Автор: Parker Dean E., Perrott Chad A., Rippstein Ryan A.
Принадлежит:

Methods of processing bio-based material feed (“bio-feed”) and a petroleum feed, using combinations of hydrotreating beds, dewaxing beds, post-treatment beds, and liquid quenching zones. Some methods comprise processing the petroleum feed through first hydrotreating reactor beds; then processing the output with a bio-feed together through second hydrotreating reactor beds; then processing the output through the plurality of dewaxing beds to create a dewaxed stream; and, processing the dewaxed stream through the plurality of post-treatment beds to create a product stream. Other methods comprise processing the petroleum feed through the plurality of first hydrotreating reactor beds; then processing the output through the plurality of dewaxing beds to create a dewaxed stream; and, processing the dewaxed stream and the bio-feed together through the plurality of liquid quenching beds zones to create a mixed stream; and, processing the mixed stream through the plurality of post-treatment beds to create a product stream. 1. A method of processing a bio-based material feed (“bio-feed”) and a petroleum feed , the method comprising: a plurality of first hydrotreating reactor beds;', 'a plurality of second hydrotreating reactor beds;', 'a plurality of dewaxing beds; and', 'a plurality of post-treatment beds; and, 'providing one or more reactors comprising, in seriesprocessing the petroleum feed through the plurality of first hydrotreating reactor beds to create a first hydrotreated stream;processing the first hydrotreated stream and the bio-feed together through the plurality of second hydrotreating reactor beds to create a second hydrotreated stream;processing the second hydrotreated stream through the plurality of dewaxing beds to create a dewaxed stream; and,processing the dewaxed stream through the plurality of post-treatment beds to create a product stream.2. The method of wherein first hydrotreating reactor beds and the second hydrotreating reactor beds each receive a ...

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Номер записи: 64
27-01-2022 дата публикации

INTEGRATING EBULLATED BED HYDROCRACKING AND COKING UNITS

Номер: US20220025283A1
Автор: Arora Arun, Koduru Suresh B.
Принадлежит: LUMMUS TECHNOLOGY LLC

Integrated processes and systems for the production of distillate hydrocarbons and coke. The process may include feeding a hydrocarbon feedstock, comprising a residuum hydrocarbon fraction, to a residue hydrocracking reactor system to convert hydrocarbons therein, producing a hydrocracked effluent. The hydrocracked effluent may then be fed to a separation system, separating the hydrocracked effluent into one or more distillate hydrocarbon fractions and a vacuum residue fraction. The vacuum residue fraction may be fed to a coker system, converting the vacuum residue fraction into a coke product and a coker vapor effluent, recovering the coke product, and feeding the coker vapor effluent to the separation system. The one or more distillate hydrocarbon fractions are hydroprocessed to produce a hydroprocessed effluent, and the hydroprocessed effluent is separated into product distillate hydrocarbon fractions. 1. A process for the production of distillate hydrocarbons and coke , the process comprising:feeding a hydrocarbon feedstock, comprising a residuum hydrocarbon fraction, to a residue hydrocracking reactor system to convert hydrocarbons therein, producing a hydrocracked effluent;in a separation system, separating the hydrocracked effluent into one or more distillate hydrocarbon fractions and a vacuum residue fraction;in a coker system, converting the vacuum residue fraction into a coke product and a coker vapor effluent, recovering the coke product, and feeding the coker vapor effluent to the separation system;hydroprocessing the one or more distillate hydrocarbon fractions to produce a hydroprocessed effluent; andseparating the hydroprocessed effluent into product distillate hydrocarbon fractions.2. The process of claim 1 , comprising feeding a straight run vacuum residue to the separation system.3. The process of claim 1 , wherein the residue hydrocracking reactor system comprises one or more ebullated bed reactors.4. The process of claim 1 , wherein the ...

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Номер записи: 65
11-01-2018 дата публикации

Supercritical Water Separation Process

Номер: US20180010057A1
Автор: Coppola Edward N., JR. Charles, Nana Sanjay, Pelt Kenneth D., Red, Wahlgren Jocelyn Marie
Принадлежит:

A supercritical water separation process and system is disclosed for the removal of metals, minerals, particulate, asphaltenes, and resins from a contaminated organic material. The present invention takes advantage of the physical and chemical properties of supercritical water to effect the desired separation of contaminants from organic materials and permit scale-up. At a temperature and pressure above the critical point of water (374° C., 22.1 MPa), nonpolar organic compounds become miscible in supercritical water (SCW) and polar compounds and asphaltenes become immiscible. The process and system disclosed continuously separates immiscible contaminants and solids from the supercritical water and clean oil product solution. The present invention creates a density gradient that enables over 95% recovery of clean oil and over 99% reduction of contaminants such as asphaltenes and particulate matter depending on the properties of the contaminated organic material. 1. A process for separating contaminants from a contaminated feedstock comprised of:combining a contaminated feedstock and supercritical water to form a supercritical water and feedstock solution in a hydrothermal separation vessel, said hydrothermal separation vessel including an upper separation zone and a bottom concentration zone;maintaining a temperature and pressure within the hydrothermal separation vessel to achieve a vertical density gradient therein such that the separation zone of the hydrothermal separation vessel exhibits a lower density than the concentration zone of the hydrothermal separation vessel, to cause the contaminants to separate from the solution in the separation zone and to form a product stream;removing the product stream from the separation zone of the hydrothermal separation vessel; andremoving the contaminants from the concentration zone of the hydrothermal separation vessel.2. The process of claim 1 , wherein the separation zone is maintained at a pressure greater than 22.1 MPa ...

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Номер записи: 66
14-01-2021 дата публикации

POWER RECOVERY FROM QUENCH AND DILUTION VAPOR STREAMS

Номер: US20210009904A1
Автор: Couch Keith Allen, Eizenga Donald A., Frey Stanley Joseph, Harris James W.
Принадлежит:

A process for reducing pressure of a vapor stream used for reducing a temperature or pressure in a reactor. A pressure of a vapor stream is reduced with a turbine to provide a lower pressure vapor stream. The vapor stream rotates a turbine wheel within the turbine. The turbine wheel is configured to transmit rotational movement to an electrical generator. Thus, electricity is generated with the turbine. The lower pressure vapor stream is injected into a reactor and reduces a temperature in the reactor or reduces a partial pressure of a hydrocarbon vapor in the reactor. 1. A process comprising: reducing a pressure of the vapor stream with a turbine to provide a lower pressure vapor stream, wherein the vapor stream comprises hydrogen;', 'rotating a turbine wheel within the turbine; and,', 'injecting the lower pressure vapor stream into the reactor and reducing the temperature in the reactor, wherein the reactor comprises an FCC reactor, and wherein the vapor stream comprises a steam stream,, 'reducing an amount of a vapor stream used for reducing a temperature, or heat load, in a reactor relative to a control valve bywherein the reactor comprises an FCC reactor, and wherein the vapor stream comprises a steam stream.2. A process comprising: providing a vapor stream comprising steam;', 'passing the vapor stream through a turbine, the turbine comprising a turbine wheel within the turbine; and,', 'reducing a partial pressure of a hydrocarbon vapor by mixing the reduced pressure vapor stream with the hydrocarbon vapor., 'reducing pressure of a vapor stream used for adjusting a partial pressure of a hydrocarbon vapor by3. The process of claim 1 , wherein the reduced pressure vapor stream is injected into an FCC reactor to reduce the partial pressure of the hydrocarbon vapor in the FCC reactor.4. The process of further comprising:recovering electricity generated with the turbine.5. The process of further comprising:adjusting one or more process conditions for the FCC reactor ...

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Номер записи: 67
10-01-2019 дата публикации

Multi-Stage Process and Device Utilizing Structured Catalyst Beds for Production of a Low Sulfur Heavy Marine Fuel Oil

Номер: US20190010408A1
Автор: Klussmann Bertrand Ray, Moore Michael Joseph, White Carter James
Принадлежит: Mag&#275;m&#257; Technology, LLC

A multi-stage process for the distributive production of an ISO 8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core process under reactive conditions in a Reaction System composed of one or more reaction vessels, wherein one or more of the reaction vessels contains one or more catalysts in the form of a structured catalyst bed. The Product Heavy Marine Fuel Oil has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed that can utilize the one or more reaction vessels, wherein one or more of the reaction vessels contains one or more catalysts in the form of a structured catalyst bed. 1. A process for the production of a Product Heavy Marine Fuel Oil , the process comprising: mixing a quantity of Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a Feedstock Mixture; contacting the Feedstock Mixture with one or more catalysts under reactive conditions to promote the formation of a Process Mixture from said Feedstock Mixture , wherein said one or more catalysts are in the form of a structured catalyst bed; receiving said Process Mixture and separating the liquid components of the Process Mixture from the bulk gaseous components of the Process Mixture; and separating any residual gaseous components and by-product hydrocarbon components from the Product Heavy Marine Fuel Oil.2. The process of claim 1 , wherein the structured catalyst bed comprises a plurality of catalyst retention structures claim 1 , each catalyst retention structure composed of a pair of fluid permeable corrugated metal sheets claim 1 , wherein the pair of the fluid permeable corrugated metal sheets are aligned such that the corrugations are out of phase and thereby defining a catalyst rich space and a catalyst lean space within the structured catalyst bed claim 1 , ...

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Номер записи: 68
10-01-2019 дата публикации

PROCEDURE FOR PREPARATION OF IMPROVED SOLID HYDROGEN TRANSFER AGENTS FOR PROCESSING HEAVY AND EXTRA-HEAVY CRUDE OILS AND RESIDUES, AND RESULTING PRODUCT

Номер: US20190010409A1
Автор: ALEMÁN VÁZQUEZ Laura Olivia, ANCHEYTA JUÁREZ Jorge, TORRES MANCERA León Pablo
Принадлежит:

The present invention relates to the process for preparing improved solid hydrogen transfer agents obtained from a polymer with units containing the structure of naphthalene, phenanthrene or anthracene, which exhibit activity as hydrogen transfer agents in any chemical reduction reaction involving the breaking of double bonds and in treatment, hydrotreatment and hydrodisintegration reactions of heavy and extra-heavy crude oils and of cuts and currents derived therefrom. These improved solid hydrogen transfer agents can be supported and not supported on metal oxides such as boehmite, alumina, silica, titania, kaolin and/or mixture thereof, in the presence of reducing agents such as hydrogen, methane, or natural gas. In addition, the application of these improved solid hydrogen transfer agents obtained from a polymer with units containing the structure of naphthalene, phenanthrene or anthracene, it allows to improve properties of the crudes such as viscosity, decrease in the formation of coke, increase in the yield of distillates and in API gravity. These hydrogen transfer agents, being solid, can be reused and recovered from the reaction medium; they also have a thermal stability such that it can carry out reactions at temperatures up to 450° C. 1. A process for preparing improved solid hydrogen transfer agents for the processing of heavy or extra-heavy crudes or residues , characterized by it comprises the following steps: a) preparing the raw materials by grinding in a porcelain mortar AlO (OH) (Boehmite) SiO2 , Al2O3 , kaolin , preferably the Boehmite and a polymer with units containing the structure of naphthalene or phenanthrene or anthracene , preferably the naphthalene when sieving these raw materials through a mesh 165 (0.089 mm); b) prepare the physical mixture of the materials indicated in part a) , wherein , to the grinded and sieved Boehmite , distilled water is added and mixed until it forms a paste , later , it is peptized by adding an aqueous solution ...

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Номер записи: 69
09-01-2020 дата публикации

LUBRICANT BASESTOCK PRODUCTION WITH ENHANCED AROMATIC SATURATION

Номер: US20200010772A1
Автор: Dandekar Ajit B., Fingland Bradley R., Fruchey Kendall S., Weigel Scott J.
Принадлежит:

Systems and methods are provided for producing lubricant basestocks having a reduced or minimized aromatics content. A first processing stage can perform an initial amount of hydrotreating and/or hydrocracking. A first separation stage can then be used to remove fuels boiling range (and lower boiling range) compounds. The remaining lubricant boiling range fraction can then be exposed under hydrocracking conditions to a USY catalyst including a supported noble metal, such as Pt and/or Pd. The USY catalyst can have a desirable combination of catalyst properties, such as a unit cell size of 24.30 or less (or 24.24 or less), a silica to alumina ratio of at least 50 (or at least 80), and an alpha value of 20 or less (or 10 or less). In some aspects, the effluent from the second (hydrocracking) stage can be dewaxed without further separation. In such aspects, a portion of the dewaxed effluent can be used as a recycle quench stream to cool the hydrocracking effluent prior to entering the dewaxing reactor. 113.-. (canceled)14. A system for producing a lubricant boiling range product , comprising:a hydrotreating reactor comprising a hydrotreating feed inlet, a hydrotreating effluent outlet, and at least one fixed catalyst bed comprising a hydrotreating catalyst;a separation stage having a first separation stage inlet and a second separation stage inlet, the first separation stage inlet being in fluid communication with the hydrotreating effluent outlet, the separation stage further comprising a plurality of separation stage liquid effluent outlets, one or more of the separation stage liquid effluent outlets corresponding to product outlets;a hydrocracking reactor comprising a hydrocracking feed inlet, a hydrocracking effluent outlet, and at least one fixed catalyst bed comprising a hydrocracking catalyst, the hydrocracking feed inlet being in fluid communication with at least one separation stage liquid effluent outlet, and the hydrocracking catalyst comprising USY zeolite ...

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Номер записи: 70
03-02-2022 дата публикации

HYDROCRACKING CATALYSTS CONTAINING RARE EARTH CONTAINING POST-MODIFIED USY ZEOLITE, METHOD FOR PREPARING HYDROCRACKING CATALYSTS, AND METHOD FOR HYDROCRACKING HYDROCARBON OIL WITH HYDROCRACKING CATALYSTS

Номер: US20220032273A1
Автор: Hodgkins Robert Peter, KOSEOGLU Omer Refa, Uchida Koji, Watabe Mitsunori
Принадлежит:

In accordance with one or more embodiments of the present disclosure, a catalyst composition includes a catalyst support and at least one hydrogenative component disposed on the catalyst support. The catalyst support includes at least one USY zeolite having a framework substituted with titanium and zirconium. The framework-substituted USY zeolite comprises at least one rare earth element. Methods of making and using such a catalyst in a hydrocracking process are also disclosed. 1. A catalyst composition comprising:a catalyst support comprising at least one framework-substituted ultra-stable Y-type (USY) zeolite substituted with zirconium atoms and titanium atoms, the at least one framework-substituted USY zeolite comprising at least one doped rare earth element; andat least one hydrogenative component disposed on the catalyst support.2. The catalyst composition of claim 1 , wherein the at least one framework-substituted USY zeolite is substituted with 0.1 wt. % to 5 wt. % zirconium atoms and 0.1 wt. % to 5 wt. % titanium calculated on an oxide basis.3. The catalyst composition of claim 1 , wherein the rare earth element is selected from the group consisting of scandium claim 1 , yttrium claim 1 , lanthanum claim 1 , cerium 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 claim 1 , lutetium claim 1 , and a combination of two more thereof.4. The catalyst composition of claim 1 , wherein the framework-substituted USY zeolite comprises a crystal lattice constant from 2.43 nm to 2.45 nm.5. The catalyst composition of claim 1 , wherein the framework-substituted USY zeolite comprises a specific surface area from 600 m/g to 900 m/g.6. The catalyst composition of claim 1 , wherein the catalyst composition comprises a specific surface area from 200 m/g to 450 m/g.7. The catalyst composition of ...

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Номер записи: 71
03-02-2022 дата публикации

Feed Flexible Hydrocracking Operations

Номер: US20220033723A1
Автор: KOMALARAJUN Varut, Maesen Theodorus Ludovicus Michael
Принадлежит: Chevron U.S.A. INC.

A hydrocracking process for converting a petroleum feed to lower boiling products. The process comprises hydrotreating a petroleum feed in a pre-treating zone in the presence of hydrogen to produce a hydrotreated effluent stream comprising a liquid product. At least a portion of the hydrotreated effluent stream is then passed to an MMS catalyst zone, and then to a hydrocracking zone. In one embodiment, the MMS catalyst zone comprises a self-supported multi-metallic catalyst prepared from a precursor in the oxide or hydroxide form. The percentage work of the hydrotreating in the pre-treating zone is maintained at a level of at least 56%. 1. A hydrocracking process for converting a petroleum feed to lower boiling products ,which process comprises:(i) hydrotreating a petroleum feed in the presence of hydrogen in a pre-treating zone to produce a hydrotreated effluent stream comprising a liquid product;(ii) passing the hydrotreated effluent stream to an MMS catalyst zone comprising an MMS catalyst for reaction to create a resulting effluent; and(iii) passing at least a portion of the resulting effluent from (ii) to a hydrocracking zone having a reaction zone to produce a hydrocracked effluent stream;with a work percentage for the pre-treating zone (i) maintained at a level of at least 56%.2. The process of claim 1 , wherein the MMS catalyst in the MMS catalyst zone in (ii) comprises a self-supported multi-metallic catalyst prepared from a precursor in the oxide or hydroxide form.3. The process of claim 2 , wherein the MMS catalyst in the MMS catalyst zone comprises a self-supported multi-metallic catalyst prepared from a precursor in the hydroxide form.4. The process of claim 2 , wherein the hydrocracked effluent is passed to a distillation column.5. The process of claim 2 , wherein the hydrocracking zone comprises up to three reaction zones.6. The process of claim 5 , wherein effluent from a bottom reaction zone is passed to a distillation column.7. The process of claim ...

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Номер записи: 72
19-01-2017 дата публикации

A process for the preparation of a feedstock for a hydroprocessing unit

Номер: US20170015916A1
Автор: Arno Johannes Maria OPRINS, Ravichander Narayanaswamy, Thomas Hubertus Maria HOUSMANS, Vijayanand RAJAGOPALAN
Принадлежит: SABIC Global Technologies BV, Saudi Basic Industries Corp

A process for preparing a feedstock for a hydroprocessing unit, the feedstock based on crude oil containing asphaltenes and the process including mixing crude oil with a predetermined solvent in a ratio such that no aggregation of asphaltenes in the mixture takes place, and feeding the combined mixture to one or more hydroprocessing units.

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Номер записи: 73
21-01-2021 дата публикации

HYDROPROCESSING OF HEAVY CRUDES BY CATALYSTS IN HOMOGENOUS PHASE

Номер: US20210017457A1
Автор: DOMÍNGUEZ ESQUIVEL José Manuel, PORTALES MARTINEZ Benjamin, SCHACHT HERNANDEZ Persi, SOTO ESCALANTE Ismael
Принадлежит:

This disclosure relates to a procedure, which through the application of a catalyst in homogeneous phase, allows the transformation of heavy hydrocarbons (vacuum residue, atmospheric residue, heavy and extra-heavy crudes) into hydrocarbons of lower molecular weight, characterized because after its application, the hydrocarbons obtain greater API gravity, lower kinematic viscosity and different composition by hydrocarbon families (SARA) that increases the proportion of saturated and aromatic resins and asphalts. The sulphur and nitrogen content is also reduced, resulting in higher yields to high commercial value distillates and a lighter product as compared to the original crude. 1. A catalyst to transform heavy and extra-heavy crude oils into lighter oils , wherein organic metal salts that includes a metal from one of Groups VIIB , VIB or IB are used for preparation of the catalyst.2. A catalyst in accordance with claim 1 , wherein the metal in the metal salt is one of Fe claim 1 , Co claim 1 , Ni claim 1 , Cu claim 1 , Mo claim 1 , or W.3. A procedure for the preparation of a catalyst claim 1 , comprising:1) mixing a mineral acid and ammonium salts, and shaking the mixture at a temperature of 25° C. until a clear solution is obtained, with a pH variation between 1 and 2;2) incorporating Nickel salts into the clear solution and solubilize at 40-100° C., then dissolving in water, and maintaining agitation of the solution for a time of 3 h at a temperature of 25° C., resulting in a green and translucent solution;3) storing the green and translucent solution in a closed container under ambient conditions; and [{'sub': '2', 'wherein the catalyst has a final molar ratio of 1.0 Ni, 0.084 Mo, 0.295 H+, 14.42 HO, at pH 1 to 3;'}, 'and wherein the catalyst transforms heavy and extra-heavy crude oils into lighter oils., '4) dehydrating the catalyst at 90° C.,'}4. The procedure for the preparation of a catalyst claim 3 , in accordance with claim 3 , wherein during preparation ...

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Номер записи: 74
16-01-2020 дата публикации

INTEGRATED THERMAL PROCESS FOR HEAVY OIL AND GAS TO LIQUIDS CONVERSION

Номер: US20200017777A1
Автор: Archer Bernard Mark, Benham Kelly, Benham Nicholas Daniel
Принадлежит:

The present disclosure generally relates to upgrading difficult to process heavy-oil. In particular, the disclosure relates to upgrading heavy oil and other high carbon content materials by using an integrated thermal-process (ITP) that utilizes anti-coking management and toluene insoluble organic residues (TIOR) management to directly incorporate lighter hydrocarbons into high molecular weight, low hydrogen content hydrocarbons such as thermally processed heavy oil products. This process can be integrated with other thermal processing schemes, such as cokers and visbreakers, to improve the conversion and yields from these integrated processes. 1331-. (canceled)332. A reactor unit for upgrading a hydrocarbon-feedstock , the reactor unit comprising:i) a first end;ii) a second end;iii) a sidewall that defines a plenum between the first end and the second end;iv) an anti-coking additive inlet that is configured to introduce an anti-coking additive into the plenum;v) a feedstock inlet that is configured to introduce a low hydrogen-content hydrocarbon feedstock into the plenum proximal the first end;vi) a first gas-inlet that is configured to introduce a high hydrogen-content light hydrocarbon gas mixture having an average molecular weight of at least 5 into the plenum at an inlet temperature of at least about 800° F.; andvii) a first outlet that is configured to remove a mixed effluent from the plenum proximal the second end.333. The reactor unit of claim 332 , wherein the high hydrogen-content light hydrocarbon gas mixture has an average molecular weight of at least 8.334. The reactor unit of claim 332 , wherein the high hydrogen-content light hydrocarbon gas mixture has an average molecular weight of at least 15.335. The reactor unit of claim 332 , wherein the first gas-inlet has a nozzle exit velocity of at least 200 ft/second.336. The reactor unit of claim 335 , wherein the first gas-inlet has a nozzle exit velocity of between 300 and 500 ft/second.337. The reactor ...

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Номер записи: 75
28-01-2016 дата публикации

PROCESS FOR PRODUCING HYDROCARBONS

Номер: US20160024391A1
Автор: ALKILDE Ole Frej, Christensen Thomas Sandahl
Принадлежит:

The invention relates to a process for the production of liquid hydrocarbons by the use of light-end fractions from downstream synthesis in the reforming section of the plant. 1. Process for the production of liquid hydrocarbons from a hydrocarbon feedstock comprising:(a) combining a light-end fraction stream from the upgrading stage of step (g) with a stream of natural gas to form said hydrocarbon feedstock;(b) passing said hydrocarbon feedstock through a hydrogenation stage to form a hydrogenated feedstock;(c) passing the hydrogenated feedstock through a desulfurization stage to form a desulfurized feedstock;(d) passing the desulfurized feedstock through a pre-reforming stage under the addition of steam to form a pre-reformed gas;(e) passing the pre-reformed gas through an autothermal reformer (ATR) or Catalytic Partial Oxidation unit (CPO) under the addition of an oxidant gas to form a synthesis gas;(f) passing the synthesis gas through a Fischer-Tropsch synthesis stage to form a tail gas stream and a raw product stream of hydrocarbons;(g) passing the raw product stream of hydrocarbons through an upgrading stage to form a final product stream of liquid hydrocarbons and a light-end fraction stream, in which the light-end fraction stream comprises a C1-C6 fraction and C6+ fraction containing paraffinic and olefinic hydrocarbons, but no naphtha.2. Process according to in which the upgrading stage (g) comprises hydrocracking but no hydrotreating.3. Process according to in which the light-end fraction stream is liquefied petroleum gas (LPG) constituted by a C2-C6 fraction.4. Process according to in which the hydrogenation of step (b) is conducted under the addition of hydrogen to the hydrocarbon feedstock.5. Process according to in which the pre-reforming stage is conducted adiabatically in a fixed bed of nickel catalyst.6. Process according to in which the ATR or CPO stage is conducted in a fixed bed of nickel catalyst in which the active component is not solely a ...

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Номер записи: 76
28-01-2016 дата публикации

Hydrocarbon Pyrolysis Process

Номер: US20160024397A1
Автор: Keusenkothen Paul F., Stell Richard C.
Принадлежит:

Disclosed is a pyrolysis process that is capable of being with reduced coke and/or tar formation. The process can pyrolyze hydrocarbon feed that contains low- to mid-range levels of non-volatiles. Pyrolysis is carried out with a predetermined amount of the feed being in the liquid phase so as to minimize coke and/or tar formation in the pyrolysis reactor. The pyrolysis feed may also include a diluent, such as molecular hydrogen, that further acts to minimize coke and/or tar formation in the pyrolysis reactor. The amount of diluent in the pyrolysis feed can be adjusted to adjust or control dry point of the hydrocarbon in the pyrolysis feed. 1. A regenerative reactor system comprising: a housing enclosing an interior region;', 'one or more process flow components configured to manage the flow of a pyrolysis stream through the interior region, wherein the one or more process flow components comprise one or more reactor beds;, 'a reverse flow regenerative reactor comprisinga pyrolysis inlet conduit having an internal surface and in fluid communication with the reverse flow regenerative reactor, whereby the pyrolysis inlet conduit is configured to manage the flow of the pyrolysis stream to the reverse flow regenerative reactor; anda liquid distribution device disposed along the flow path of the pyrolysis stream and in fluid communication with the pyrolysis inlet conduit, whereby the liquid distribution device is configured to disperse a liquid portion of the pyrolysis stream along the internal surface of the pyrolysis inlet conduit.2. The regenerative reactor system of claim 1 , wherein the reverse flow regenerative reactor further comprises one or more structural members disposed within the internal region and near the pyrolysis inlet conduit to lessen fouling near the pyrolysis inlet conduit within the internal region.3. The regenerative reactor system of claim 1 , further comprising a non-combustible non-volatile removal unit upstream of the pyrolysis inlet conduit ...

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Номер записи: 77
28-01-2016 дата публикации

GRAVITATIONAL COLLISION ENHANCED UPGRADING OF HEAVY OILS

Номер: US20160024398A1
Автор: Ellingsen Olav
Принадлежит:

The present invention relates to gravitational collision enhanced upgrading of heavy oils, It thus describes a thermodynamic cracking process for heavy oil, extra heavy oil and bituem as well as a thermodynamic cracking unit for carrying out the process. 1. A thermodynamic cracking process of heavy oil , extra heavy oil and bitumen , characterized in that cracking is carried out in an reactor (oil cracker) having re-circulation rings under the influence two or more gravitational and accelerated jets of hot mineral heat carrier and combustion gasses , colliding jets injected at a positive angle into the lower part of the oil cracker whereby the stream will be diverted upwards introducing mechanical shear forces and hotspots which together with an operating temperature between 450 C and 600 C cracks the oil injected and atomized at the bottom of the oil cracker.2. The thermodynamic process in accordance with claim 1 , characterized in that the energy carrier is selected from fine grained minerals claim 1 , such as silica claim 1 , magnesium oxide claim 1 , aluminum oxide claim 1 , copper oxide claim 1 , anorthisite claim 1 , olivine or similar materials.3═H. The thermodynamic process in accordance with claim 1 , characterized in that hydrogen is produced in the oil cracker by the gas/water shift CO+H0+C0where the hydrogen hydrogenates the cracked oil gas in the oil cracker under the influence of cavitations due to internal remixing rings.4. The thermodynamic process in accordance with claim 1 , characterized in that the energy carrier is regenerated in a fluidized regeneration chamber having fluidizing fluidization nozzles above a plenum receiving air and where the energy carrier is regenerated by oxidizing co-accumulated coke contained therein and that the regenerator have internal recirculation rings for optimizing combustion conditions.5. The thermodynamic process in accordance with claim 4 , characterized in that the regenerator comprises a heat exchanger and a ...

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Номер записи: 78
26-01-2017 дата публикации

STAGED CATALYST LOADING FOR PYROLYSIS OIL HYDRODEOXYGENATION

Номер: US20170022425A1
Автор: Baird Lance A., Towarnicky Andrew J.
Принадлежит:

A method for deoxygenating a biomass-derived pyrolysis oil is described. The method includes combining a biomass-derived pyrolysis oil stream with a heated low-oxygen-py-oil diluent recycle stream to form a heated diluted py-oil feed stream that has a temperature of about 150° C. or greater. The heated diluted py-oil feed stream is contacted with a first deoxygenating catalyst in a first bed of a reactor to form a low-oxygen biomass-derived pyrolysis oil. The low-oxygen biomass-derived pyrolysis oil is contacted with a hydrocracking catalyst in a second bed of the reactor to form a hydrocracked low-oxygen biomass-derived pyrolysis oil effluent. A portion of the hydrocracked low-oxygen biomass-derived pyrolysis oil effluent comprises the heated low-oxygen biomass-derived py-oil diluent recycle stream. 1. A method for deoxygenating biomass-derived pyrolysis oil comprising:combining a biomass-derived pyrolysis oil stream with a heated low-oxygen-py-oil diluent recycle stream to form a heated diluted py-oil feed stream that has a temperature of about 150° C. or greater;contacting the heated diluted py-oil feed stream with a first deoxygenating catalyst in a first bed of a reactor in the presence of hydrogen at first hydroprocessing conditions effective to form a low-oxygen biomass-derived pyrolysis oil; andcontacting the low-oxygen biomass-derived pyrolysis oil with a hydrocracking catalyst in a second bed of the reactor in the presence of hydrogen at hydrocracking conditions effective to form a hydrocracked low-oxygen biomass-derived pyrolysis oil effluent;wherein a portion of the hydrocracked low-oxygen biomass-derived pyrolysis oil effluent comprises the heated low-oxygen biomass-derived py-oil diluent recycle stream.2. The method of further comprising:introducing a hydrogen stream to the reactor between the first and second beds to adjust the ratio of hydrogen to hydrocarbon in the second bed and to adjust a temperature in the second bed.3. The method of wherein ...

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Номер записи: 79
26-01-2017 дата публикации

FIXED BED HYDROPROCESSING OF DEASPHALTER ROCK

Номер: US20170022433A1
Автор: AMES Warren B., Barrai Federico, Brown Stephen H.
Принадлежит:

Systems and methods are provided for fixed bed hydroprocessing of deasphalter rock. Instead of attempting to process vacuum resid in a fixed bed processing unit, vacuum resid is deasphalted to form a deasphalted oil and deasphalter residue or rock. The rock can then be hydroprocessed in a fixed bed reaction zone, optionally after combining the rock with an aromatic co-feed and/or a hydroprocessing solvent. This can allow for improved conversion of the deasphalter rock and/or improved combined conversion of the deasphalter rock and deasphalted oil. 1. A method for fixed bed processing of deasphalter rock , comprising:exposing a feedstock comprising deasphalter rock and a co-feed comprising a catalytic slurry oil, a lubes extract, a heavy coker gas oil, a vacuum gas oil derived from a heavy oil, or a combination thereof, to a fixed bed of hydroprocessing catalyst under hydroprocessing conditions effective for conversion of at least 40 wt % of the deasphalter rock relative to a conversion temperature of 1050° F. (566° C.) to form a hydroprocessed effluent, the feedstock comprising at least about 20 wt % of the co-feed and at least about 10 wt % of the deasphalter rock.2. The method of claim 1 , wherein the feedstock comprises at least about 30 wt % of the deasphalter rock.3. The method of claim 1 , further comprising performing solvent deasphalting on a resid feedstock to form at least the deasphalter rock and a deasphalted oil fraction claim 1 , the resid feedstock having a T10 distillation point of at least about 650° F. (˜343° C.) claim 1 , the deasphalter rock comprising at least about 10 wt % of the resid feedstock.4. The method of claim 1 , wherein the feedstock comprises at least about 20 wt % of the catalytic slurry oil.5. The method of claim 1 , wherein the feedstock comprises at least about 30 wt % of the co-feed.6. The method of claim 1 , wherein the feedstock further comprises an aromatic solvent claim 1 , the aromatic comprising at least 50 wt % of ...

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Номер записи: 80
24-01-2019 дата публикации

HYDROCRACKING CATALYST FOR HYDROCARBON OIL, METHOD FOR PRODUCING HYDROCRACKING CATALYST, AND METHOD FOR HYDROCRACKING HYDROCARBON OIL WITH HYDROCRACKING CATALYST

Номер: US20190022630A1
Автор: "Al-AbdulAl Ali H.", AI-THUKAIR Mishaal, Al-Hajji Adnan, AL-SOMALI Ali Mahmoud, Kameoka Takashi, KOSEOGLU Omer Refa, Kuroda Ryuzo, Nakano Koji, Takamori Yuichi, Ushio Masaru
Принадлежит:

The present invention relates to a hydrocracking catalyst for hydrocarbon oil comprising a support containing a framework-substituted zeolite-1 in which zirconium atoms and/or hafnium atoms form a part of a framework of an ultrastable y-type zeolite and a hydrogenative metal component carried thereon and a method for producing the same. The hydrocracking catalyst of the present invention makes it easy to diffuse heavy hydrocarbon oils such as VGO, DAO and the like into mesopores, is improved in a cracking activity and makes it possible to obtain a middle distillate at a high yield as compared with catalysts prepared by using zeolite comprising titanium and/or zirconium carried thereon. 120-. (canceled)21. A hydrocracking catalyst for the high boiling fraction containing hydrocarbon oil comprising a hydrogenative metal component carried on a support containing an ultra-stable Y-type zeolite ,wherein the ultra-stable Y-type zeolite is a framework-substituted zeolite (hereinafter referred to as a framework-substituted zeolite-1) in which a part of aluminum atoms constituting a zeolite framework thereof is substituted with zirconium atoms and/or hafnium atoms,said zeolite-1 has a crystallinity of 80% or more, and contains from 0.1 to 5 mass % zirconium atoms and/or hafnium atoms as calculated as the oxide basis, anda relative decomposition rate as defined below is 99% or more, and a relative middle distillate yield as defined below is 95% or more:(Relative decomposition rate and relative middle distillate yield){'sup': −1', '3, 'claim-text': [{'br': None, 'Decomposition rate (%)={1−(Content (kg) of a fraction having a boiling point of higher than 375° C. in the produced oil/Content (kg) of a fraction having a boiling point of higher than 375° C. in the raw oil)}×100\u2003\u2003Equation (2), {'br': None, 'Middle distillate yield (%)={Content (kg) of a fraction having a boiling point of 149 to 375° C. in the produced oil/Content (kg) of a fraction having a boiling point ...

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Номер записи: 81
10-02-2022 дата публикации

PROCESS FOR POLYMER MIXTURE HYDROCONVERSION

Номер: US20220041937A1
Автор: BALDUCCI Daniele, Guidetti Stefania, MARIANI Paolo, Scavello Francesco, VECCHINI Nicola
Принадлежит:

There is a process for the hydroconversion of mixtures of polymers or plastics which comprises the pre-treatment of the mixtures through methods selected from mechanical methods, chemical methods, thermal methods, or combinations thereof forming a pre-treated charge. The pre-treated charge is mixed with a hydrocarbon vacuum residue, optionally pre-heated, to form a reactant mixture. The reactant mixture is fed to a hydroconversion section in slurry phase, together with a catalyst precursor containing Molybdenum, and a stream containing hydrogen, forming a reaction effluent. The effluent is separated into at least one high-pressure and high-temperature separator in a vapour phase and a slurry phase. The separate vapour phase is sent to a gas treatment section with the function of separating a liquid fraction from the gas containing hydrogen and hydrocarbon gases having from 1 to 4 carbon atoms; said liquid fraction comprising naphtha, atmospheric gas oil (AGO), vacuum gas oil (VGO). The slurry phase is then sent to a separation section that has the function of separating the fractions of the Vacuum Gas Oil (VGO), Heavy Vacuum Gas Oil (HVGO), Light Vacuum Gas Oil (LVGO), Atmospheric Gas Oil (AGO), from a stream of heavy organic products which contains asphaltenes, unconverted charge, catalyst and solid formed during the hydroconversion reaction. This stream of heavy organic products is partly recirculated to the hydroconversion section and partly forms a purge stream. 1. A process for polymer mixture hydroconversion which comprises the following steps:pre-treating a polymer mixture through methods selected from mechanical methods, chemical methods, thermal methods, or combinations thereof, forming a pre-treated charge;mixing said pre-treated charge with a vacuum hydrocarbon residue, optionally pre-heated, to form a reactant mixture;feeding to a hydroconversion section the reactant mixture in slurry phase, a precursor of the catalyst containing Molybdenum, and a stream ...

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Номер записи: 82
24-01-2019 дата публикации

PROCESS FOR COMBINED HYDRODESULFURIZATION AND HYDROCRACKING OF HEAVY HYDROCARBONS

Номер: US20190023996A1
Автор: Aramburo Luis, VAN KIMMENADE Emiel
Принадлежит:

The present invention relates to a process for combined hydrodesulfurization and hydrocracking of a heavy hydrocarbon feed comprising contacting the hydrocarbon feed in the presence of hydrogen with a catalyst comprising a mixture of a solid acid catalyst and a hydrodesulfurization catalyst. 1. A process for combined hydrodesulfurization and hydrocracking of a heavy hydrocarbon feed comprising:contacting said heavy hydrocarbon feed in the presence of hydrogen at process conditions comprising a temperature of 350-475° C. and a pressure of 2500-4500 kPa, with a catalyst comprising a mixture of a solid acid catalyst and a hydrodesulfurization catalyst,wherein said hydrodesulfurization catalyst comprises 1-30 wt-% of an element selected from Group 6 of the Periodic Table of Elements based on the total weight of the hydrodesulfurization catalyst, and 0.1-10 wt-% of an element selected from Groups 9 and 10 of the Periodic Table of Elements based on the total weight of the hydrodesulfurization catalyst and a solid catalyst support, and{'sub': 2', '2', '3, 'wherein said solid acid catalyst is comprises an aluminosilicate zeolite having a SiO/AlOmolar ratio of 50-120.'}2. The process according to claim 1 , wherein the element selected from Groups 9 and 10 of the Periodic Table of Elements is Co and/or Ni.3. The process according to claim 1 , wherein the element in the hydrodesulfurization catalyst is in sulfide form.4. The process according to claim 1 , wherein the hydrodesulfurization catalyst comprises one or more selected from the group consisting of CoMoS claim 1 , NiMoS claim 1 , NiWSand CoWS.5. The process according to claim 1 , wherein the solid acid catalyst comprises aluminosilicate zeolite having a 12-ring structure.6. The process according to claim 5 , wherein the aluminosilicate zeolite has super cages having a size of 12-14 Å.7. The process according to claim 5 , wherein the aluminosilicate zeolite is zeolite Y.8. The process according to claim 5 , wherein the ...

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Номер записи: 83
24-04-2014 дата публикации

High rate reactor system

Номер: US20140109465A1
Автор: Charles Red, JR., Edward N. COPPOLA, Sanjay Nana
Принадлежит: Applied Research Associates Inc

A process and system for upgrading an organic feedstock including providing an organic feedstock and water mixture, feeding the mixture into a high-rate, hydrothermal reactor, wherein the mixture is rapidly heated, subjected to heat, pressure, and turbulent flow, maintaining the heat and pressure of the mixture for a residence time of less than three minutes to cause the organic components of the mixture to undergo conversion reactions resulting in increased yields of distillate fuels, higher-quality kerosene and diesel fuels, and the formation of high octane naphtha compounds. Hydrocarbon products are cooled at a rate sufficient to inhibit additional reaction and recover of process heat, and depressurizing the hydrocarbon products, and separating the hydrocarbon products for further processing. The process and system can include devices to convert olefinic hydrocarbons into paraffinic hydrocarbons and convert olefinic byproduct gas to additional high-octane naphtha and/or heavier hydrocarbons by one of hydrogenation, alkylation, or oligomerization.

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Номер записи: 84
10-02-2022 дата публикации

SYSTEMS AND METHODS FOR HOLISTIC LOW CARBON INTENSITY FUEL PRODUCTION

Номер: US20220043406A1
Автор: Herold Gregory, Whikehart David
Принадлежит: MARATHON PETROLEUM COMPANY LP

Systems and methods to provide low carbon intensity (CI) transportation fuels through one or more targeted reductions of carbon emissions based upon an analysis of carbon emissions associated with a combination of various options for feedstock procurement, feedstock refining, processing, or transformation, and fuel product distribution pathways to end users. Such options are selected to maintain the total CI (carbon emissions per unit energy) of the transportation fuel below a pre-selected threshold that defines an upper limit of CI for the transportation fuel. 1. A process to provide a low carbon intensity (CI) transportation fuel obtained through one or more targeted reductions of carbon emissions associated with a combination of various feedstock procurement , feedstock transportation , feedstock refining and fuel product distribution pathways , the process comprising:selecting a carbon intensity threshold to define an upper limit for carbon intensity of a transportation fuel to be provided to an end user location that qualifies the transportation fuel as a low carbon intensity transportation fuel;selecting a refinery feedstock that is procured at a source for transport, the refinery feedstock being selected to reduce carbon emissions associated therewith and thereby maintain the carbon intensity of the transportation fuel below the carbon intensity threshold;selecting a transportation mode to transport the refinery feedstock from the source to a refinery, the transportation mode being selected to reduce carbon emissions associated therewith and thereby maintain the carbon intensity of the transportation fuel below the carbon intensity threshold;selecting refinery processes to reduce carbon emissions associated with refining the refinery feedstock to a plurality of refined products and thereby maintain the carbon intensity of the transportation fuel below the carbon intensity threshold;refining the refinery feedstock into one or more of the plurality of refined ...

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Номер записи: 85
24-04-2014 дата публикации

Multi-stage hydrocarcking proess for the hydroconversion of hydrocarbonaceous feedstocks

Номер: US20140110306A1
Автор: Nicolaas Van Dijk
Принадлежит: Shell Oil Co

A process for the hydroconversion of a hydrocarbon feedstock. The process includes contacting the hydrocarbon feedstock with a catalyst in a first hydrocracking section to obtain a first hydrocarbon effluent stream which is separated into a gaseous stream, a light liquid stream and a heavy liquid stream. These liquid streams are fractioned into a number of fractions of hydrocarbons including a fraction of hydrocarbons having a boiling point above 350° C. This fraction of hydrocarbons is contacted with a catalyst in a second hydrocracking section to obtain a second hydrocarbon effluent stream that is separated to obtain a gaseous stream, a light liquid stream and a heavy liquid stream. These liquid streams are fractioned into a number of fractions of hydrocarbons including a heavy fraction of hydrocarbons having a boiling point above 350° C. This fraction of hydrocarbons is split into a major stream and a minor stream with the major stream being recycled and the minor stream is recovered.

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Номер записи: 86
23-01-2020 дата публикации

PROCESS FOR THE PRODUCTION OF OLEFINS AND OF MIDDLE DISTILLATES FROM A HYDROCARBON EFFLUENT RESULTING FROM THE FISCHER-TROPSCH SYNTHESIS

Номер: US20200024528A1
Автор: ETIENNE Pascal, Heraud Jean-Philippe
Принадлежит: IFP ENERGIES NOUVELLES

Process for the production of olefins and of middle distillates from a paraffinic feedstock, in which: 1. Process for the production of olefins and of middle distillates from a paraffinic feedstock produced by Fischer-Tropsch synthesis comprising at least the following stages:a) the said paraffinic feedstock resulting from a Fischer-Tropsch unit (A) is recovered, the said paraffinic feedstock comprising at least a light fraction, known as condensate, and a heavy fraction, known as waxes;b) at least a part of the said light fraction is sent to a catalytic cracking unit (C);c) the effluent resulting from the catalytic cracking unit is separated in a fractionation unit (D) in order to obtain at least a fraction comprising light hydrocarbons, at least an olefinic fraction and at least a residual liquid fraction;d) at least a part of the said heavy fraction is sent to a hydrocracking/hydroisomerization unit (F) in the presence of hydrogen and of a hydrocracking/hydroisomerization catalyst;e) the effluent resulting from the hydrocracking/hydroisomerization unit is separated in a fractionation unit (G) in order to obtain a middle distillates fraction, a naphtha cut having a maximum boiling point of less than 180° C. and an unconverted heavy fraction;f) at least a part of the said naphtha cut resulting from the fractionation unit is sent to the catalytic cracking unit.2. Process according to claim 1 , in which:an additional stage a′) is carried out in which the said light fraction obtained in stage a) is fractionated in a fractionation unit (H) in order to obtain a light cut of the said light fraction, the final boiling point of which is less than 180° C., and a heavy cut of the said light fraction, the initial boiling point of which is greater than 120° C.;a stage b) is carried out in which the said light cut of the said light fraction resulting from stage a′) is sent to the said catalytic cracking unit (C).3. Process according to claim 2 , in which an additional stage a″) ...

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Номер записи: 87
23-01-2020 дата публикации

STORAGE OF FISCHER-TROPSCH EFFLUENTS

Номер: US20200024529A1
Автор: GREZAUD Aline, Heraud Jean-Philippe
Принадлежит: IFP ENERGIES NOUVELLES

Process for the production of middle distillates from a paraffinic feedstock produced by Fischer-Tropsch synthesis comprising at least one light fraction, known as condensate, and a heavy fraction, known as waxes, in which: 1. Process for the production of middle distillates from a paraffinic feedstock produced by Fischer-Tropsch synthesis comprising at least the following stages:{'b': 2', '3, 'a) the said paraffinic feedstock resulting from a Fischer-Tropsch unit (A) is recovered, the said paraffinic feedstock comprising at least a light fraction (), known as condensate, and a heavy fraction (), known as waxes;'}{'b': 4', '5, 'b) a least a part of the said light fraction and at least a part of the said heavy fraction which are obtained on conclusion of stage a) are sent, as a mixture (), to a hydrotreating unit (D) in the presence of hydrogen and a hydrotreating catalyst in order to obtain a first hydrotreated effluent ();'}{'b': 5', '6, 'c) at least a part of the first hydrotreated effluent () obtained on conclusion of stage b) is sent to a hydrocracking/hydroisomerization unit (E) in the presence of hydrogen and of a hydrocracking/hydroisomerization catalyst in order to obtain a second effluent ();'}{'b': 6', '7', '8', '9', '10, 'd) the second effluent () resulting from the hydrocracking/hydroisomerization unit is separated in a fractionation unit (F) in order to obtain at least a naphtha cut () having a maximum boiling point of less than 180° C., a middle distillates fraction (,) and an unconverted heavy fraction ();'}which process being characterized in that, when the hydrotreating unit (D) and/or the hydrocracking/hydroisomerization unit (E) is at shutdown, then:{'b': '2', 'the said light fraction () obtained on conclusion of stage a) is stored in a vessel (B) maintained under an inert atmosphere and in which the temperature inside the vessel is maintained at a value of less than 20° C.; and/or'}{'b': '3', 'the said heavy fraction () obtained on conclusion of ...

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Номер записи: 88
29-01-2015 дата публикации

STAGED SOLVENT ASSISTED HYDROPROCESSING AND RESID HYDROCONVERSION

Номер: US20150027924A1
Автор: Barrai Federico, Brown Stephen Harold, Gupta Himanshu, TRIVEDI Kirtan Kunjbihari
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Systems and methods are provided for processing a heavy oil feed, such as an atmospheric or vacuum resid, using a combination of solvent assisted hydroprocessing and slurry hydroconversion of a heavy oil feed. The systems and methods allow for conversion and desulfurization/denitrogenation of a feed to form fuels and gas oil (or lubricant base oil) boiling range fractions while reducing the portion of the teed that is exposed to the high severity conditions present in slurry hydroconversion. 1. A method for processing a heavy oil feedstock , comprising:providing a heavy oil feedstock having a 10% distillation point of at least about 650° F. (343° C.);{'sup': '−1', 'exposing the heavy oil feedstock to a catalyst in the presence of hydrogen and a solvent under first effective hydroprocessing conditions to form an effluent comprising at least a plurality of liquid products and a hydroprocessing bottoms product, the effective hydroprocessing conditions including a temperature of at least about 360° C. and a liquid hourly space velocity of the fraction of the combined feedstock boiling above 1050° F. (566°) of at least about 0.10 hr;'}exposing the hydroprocessing bottoms product to a catalyst in the presence of hydrogen under second effective slurry hydroconversion conditions to form a slurry hydroconversion effluent comprising at least a second plurality of liquid products and a bottoms product; andfractionating the first plurality of liquid products and the second plurality of liquid products.2. The method of claim 1 , wherein the solvent component comprises a recycle component claim 1 , the process further comprising recycling a second portion of the liquid effluent to form the recycle component.3. The method of claim 2 , wherein the ratio of the recycle component to the heavy oil feed component on a weight basis is from about 0.3 to about 6.0.4. The method of claim 1 , wherein the effective hydroprocessing conditions are effective for conversion of from about 50 to ...

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Номер записи: 89
04-02-2016 дата публикации

Process for Introducing Fine and Coarse Additives for Hydroconversion of Heavy Hydrocarbons

Номер: US20160032198A1
Автор: Schleiffer Andreas, SUBRAMANIAN Anand
Принадлежит:

A process for slurry-phase hydrocracking of a heavy hydrocarbon feedstock in a reactor, such as an upflow bubble column reactor, includes separately introducing additive in two size ranges into the feedstock. A fine size particle additive is introduced upstream of a coarse size particle additive. 1. A process for slurry-phase hydrocracking of a heavy hydrocarbon feedstock in a slurry phase hydrocracking reactor , the process comprising:introducing a first additive to the feedstock upstream of a pre-heat exchanger to form a fines-loaded feedstock, the additive comprising fines particles having a particle size distribution less than 500 microns,separately introducing a second additive to the fines-loaded feedstock downstream of a feed charge pump and upstream of the slurry phase hydrocracking reactor, the second additive comprising coarse particles having a median particle size between 400 microns and 2,000 microns; andremoving reaction products from the slurry phase hydrocracking reactor.2. The process of claim 1 , wherein the slurry phase hydrocracking reactor is an upflow bubble column reactor.3. The process of claim 1 , wherein the slurry phase hydrocracking reactor is a circulating ebulated bed reactor.4. The process of claim 1 , wherein the heavy hydrocarbon feedstock comprises of a mineral oil claim 1 , synthetic oil claim 1 , heavy oil claim 1 , residual oil claim 1 , waste oil claim 1 , shale oil claim 1 , used oil claim 1 , tar sand oil claim 1 , coal oil claim 1 , coal tar claim 1 , vacuum residue claim 1 , atmospheric residue claim 1 , deasphalted bottoms claim 1 , comminuted coal claim 1 , biomass-derived materials claim 1 , and mixtures thereof.5. The process of claim 1 , wherein the heavy hydrocarbon feedstock comprises vacuum residue.6. The process of claim 1 , wherein the first additive is introduced to the feedstock in a feed mixing vessel.7. The process of claim 1 , wherein the first additive is introduced to the feedstock downstream of the feed ...

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Номер записи: 90
31-01-2019 дата публикации

METHOD FOR CONVERTING HEAVY OIL BY MEANS OF HIGH ASPHALTENE DISPERSION

Номер: US20190031966A1
Автор: CHO Joung Mo, LEE Chul Wee, Park Sun Young
Принадлежит:

The present invention relates to a method for converting heavy oil by means of high dispersion of asphaltenes, comprising the steps of: preparing a mixture by mixing an amphiphilic additive and the heavy oil; and performing a hydrogenation reaction on the mixture, wherein the amphiphilic additive comprises both a polar group and a nonpolar group. 1. A method for converting heavy oil by means of high dispersion of asphaltenes , comprising the steps of:preparing a mixture by mixing an amphiphilic additive and the heavy oil; andperforming a hydrogenation reaction on the mixture, wherein the amphiphilic additive comprises both polar and non-polar functional group.2. The method of claim 1 , wherein:the dipole moment of the polar group is greater than or equal to 1.1 Debye (D);the dipole moment of the non-polar group is less than or equal to 0.5 Debye (D); andthe net dipole moment of the amphiphilic additive is greater than or equal to 0.6 Debye (D).3. The method of claim 2 , wherein the amphiphilic additive is in the form of a polymer having a number average molecular weight of 100 to 500 claim 2 ,000.4. The method of claim 3 , wherein the polar group comprises at least one selected from amine claim 3 , imide claim 3 , amide claim 3 , alcohol claim 3 , phenol claim 3 , ester claim 3 , and methacrylate; and the non-polar group comprises a polymer induced from any one or combination of ethylene claim 3 , propylene claim 3 , isobutylene claim 3 , diene claim 3 , and styrene.5. The method of claim 2 , wherein the amphiphilic additive is used in an amount of 0.01 wt % to 5 wt % in the mixture.6. The method of claim 2 , wherein the amphiphilic additive comprises at least one from polyisobutylene succinimide claim 2 , polyisobutylene phenol-based dispersant claim 2 , and polyacrylic-based dispersant.7. The method of claim 2 , wherein the amphiphilic additive comprises a product obtained from a bottom stream in which waste oil is distilled.8. The method of claim 7 , further ...

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Номер записи: 91
11-02-2016 дата публикации

CATALYSTS POSSESSING AN IMPROVED RESISTANCE TO POISONING

Номер: US20160038920A1
Автор: Guo Xiaoyu
Принадлежит:

The present invention relates generally to the field of catalysts for use in connection with one or more types of emissions control (e.g., emissions control associated with the combustion of one or more types of fossil fuel) and, in particular to catalyst compositions that possess an improved resistance to at least one type of poisoning. In another embodiment, the catalysts of the present invention are designed to be utilized in conjunction with an SCR and possess an improved resistance to phosphorus poisoning. 1. A poison-resistant SCR catalyst composition comprising:(i) at least one vanadium compound or metal;(ii) at least one tungsten compound or metal;(iii) at least one titanium compound or metal; and(iv) at least one additional compound selected from one or more molybdenum compounds or metal,{'sub': 2', '3, 'wherein poison-resistance in the SCR catalyst is achieved due to the molar ratio of the metal portion of component (iv) to the metal portion of component (i) falling in the range of about 10:1 to about 1:1 and wherein the catalyst composition has an SOto SOconversion, or oxidation, rate that is about 2 percent or less.'}2. The catalyst composition of claim 1 , wherein the molar ratio of the metal portion of component (iv) to the metal portion of component (i) is in the range of about 9:1 to about 1:1.3. The catalyst composition of claim 1 , wherein the molar ratio of the metal portion of component (iv) to the metal portion of component (i) is in the range of about 8:1 to about 1:1.4. The catalyst composition of claim 1 , wherein the molar ratio of the metal portion of component (iv) to the metal portion of component (i) is in the range of about 7:1 to about 1:1.5. The catalyst composition of claim 1 , wherein the molar ratio of the metal portion of component (iv) to the metal portion of component (i) is in the range of about 4:1 to about 1:1.6. The catalyst composition of claim 1 , wherein the molar ratio of the metal portion of component (iv) to the metal ...

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Номер записи: 92
11-02-2016 дата публикации

FUELS HYDROCRACKING WITH DEWAXING OF FUEL PRODUCTS

Номер: US20160040083A1
Автор: DAAGE Michel, Dougherty Richard Charles, McCarthy Stephen John, Novak William J., Shih Stuart S.
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

This invention relates to a process involving hydrocracking and dewaxing of a feedstream in which a converted fraction can correspond to a majority of the product from the reaction system, while an unconverted fraction can exhibit improved properties. In this hydrocracking process, it can be advantageous for the yield of unconverted fraction for gasoline fuel application to be controlled to maintain desirable cold flow properties for the unconverted fraction. Catalysts and conditions can be chosen to assist in attaining, or to optimize, desirable product yields and/or properties. 1. A hydrocracked product of a feedstock boiling in the diesel range or above , the hydrocracked product comprising an unconverted product and a converted product , the weight of the unconverted product corresponding to from about 5 wt % to about 35 wt % of the feedstock; wherein the unconverted product stream has an initial boiling point of at least about 400° F. , a T90 boiling point of 700° F. or less , a cetane number of at least about 45 , and a cloud point at least about 10° F. less than the cloud point of the feedstock.2. The hydrocracked product of claim 1 , wherein the feedstock comprises an atmospheric gas oil claim 1 , a virgin distillate or a hydrotreated virgin distillate.3. The hydrocracked product of claim 1 , wherein the feedstock has a cetane number of about 35 or less.4. The hydrocracked product of claim 3 , wherein the cetane number of the feedstock is about 30 or less.5. The hydrocracked product of claim 1 , wherein the feedstock has a cloud point of at least 12° F.6. The hydrocracked product of claim 1 , wherein the feedstock has a cloud point of 30° F. or less.7. The hydrocracked product of claim 1 , wherein at least about 60 wt % of the feedstock boils above about 400° F.8. The hydrocracked product of claim 1 , wherein at least about 60 wt % of the feedstock boils below about 650° F.9. The hydrocracked product of claim 1 , wherein the unconverted product comprises ...

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Номер записи: 93
11-02-2016 дата публикации

BIOREFINERY SYSTEM, METHODS AND COMPOSITIONS THEREOF

Номер: US20160040198A1
Автор: Mendez Michael, Resnick Sol M., Silverman Joshua A.
Принадлежит:

The present disclosure relates to bioengineering approaches for producing biofuel and, in particular, to the use of a Cmetabolizing microorganism reactor system for converting Csubstrates, such as methane or methanol, into biomass and subsequently into biofuels, bioplastics, or the like. 1. A method for making fuel , comprising converting biomass from a culture primarily comprising a Cmetabolizing non-photosynthetic microorganism into an oil composition and refining the oil composition into a fuel.2. The method of claim 1 , wherein the oil composition is from cell membrane of the Cmetabolizing non-photosynthetic microorganism.3. The method of claim 1 , wherein the biomass is from a Cmetabolizing non-photosynthetic microorganism culture grown in a controlled culturing unit in the presence of a feedstock comprising a Csubstrate.4. The method of claim 3 , wherein the feedstock Csubstrate is methane claim 3 , methanol claim 3 , formaldehyde claim 3 , formic acid or a salt thereof claim 3 , carbon monoxide claim 3 , carbon dioxide claim 3 , syngas claim 3 , a methylamine claim 3 , a methylthiol claim 3 , or a methylhalogen.5. The method of claim 3 , wherein the controlled culturing unit is a fermentor or bioreactor.6. The method of claim 3 , wherein the culture is from a liquid-phase fermentation or a solid phase fermentation.7. The method of claim 1 , wherein the biomass is converted into an oil composition by extraction claim 1 , wherein the extraction is selected from a wet extraction claim 1 , a supercritical fluid extraction claim 1 , or a dry extraction.8. The method of claim 7 , wherein the extraction is a wet extraction claim 7 , which comprises use of a polar solvent claim 7 , non-polar solvent claim 7 , neutral solvent claim 7 , acidic solvent claim 7 , hexane claim 7 , or any combination thereof.9. The method of claim 6 , wherein the controlled culturing unit is a solid phase fermentation unit and the oil composition is extracted from the biomass by ...

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Номер записи: 94
09-02-2017 дата публикации

HYDROPROCESSING METHOD WITH HIGH LIQUID MASS FLUX

Номер: US20170037325A1
Автор: Ackerson Michael D., Byars Michael Steven
Принадлежит:

In a method of hydroprocessing, hydrogen gas for the hydroprocessing reaction is combined with a liquid feed composition comprising a feedstock to be treated and a diluent to form a feed stream, at least a portion of the hydrogen gas being dissolved in the liquid feed composition of the feed stream, with non-dissolved hydrogen gas being present in the feed stream in an amount of from 1 to 70 SCF/bbl of the liquid feed composition. The feed stream is contacted with a hydroprocessing catalyst, within a reactor while maintaining a liquid mass flux within the reactor of at least 5000 lb/hr-ftto form a hydroprocessed product. 1. A method of hydroprocessing comprising:combining hydrogen gas for the hydroprocessing reaction with a liquid feed composition comprising a feedstock to be treated and a diluent to form a feed stream, at least a portion of the hydrogen gas being dissolved in the liquid feed composition of the feed stream, with non-dissolved hydrogen gas being present in the feed stream in an amount of from 1 SCF to 70 SCF per bbl of the liquid feed composition; and{'sup': '2', 'contacting the feed stream with a hydroproces sing catalyst within a reactor while maintaining a liquid mass flux within the reactor of at least 5000 lb/hr·ftto form a hydroprocessed product.'}2. The method of claim 1 , wherein:the feedstock comprises at least one of a petroleum feedstock, a non-petroleum feedstock, a bio oil, a pyrolysis oil, a high-contaminant feedstock, and a high-olefinic feedstock.3. The method of claim 1 , wherein:the feed stream is contacted with a hydroproces sing catalyst contained in at least two catalyst beds within the reactor.4. The method of claim 1 , wherein:the non-dissolved hydrogen gas in the feed stream is present in an amount of from 1 SCF to 50 SCF per bbl of the liquid feed composition.5. The method of claim 1 , wherein:{'sup': 2', '2, 'the liquid mass flux within the reactor is maintained at from 5000 lb/hr·ftto 100,000 lb/hr·ft.'}6. The method of ...

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Номер записи: 95
08-02-2018 дата публикации

PROCESS FOR USING MOLYBDENUM AND PARTICULATE CARBON CATALYST FOR SLURRY HYDROCRACKING

Номер: US20180037826A1
Автор: Bhattacharyya Alakananda, Do Phuong T. M., Houdek Stephen C., Mezza Beckay J.
Принадлежит:

A process and catalyst is disclosed for converting heavy hydrocarbon feed into lighter hydrocarbon products using multifunctional catalysts. Multifunctional catalysts enable use of less expensive metal by substituting expensive metals for less expensive metals with no loss or superior performance in slurry hydrocracking. Less available and expensive ISM can be replaced effectively. 1. A process for converting heavy hydrocarbon feed into lighter hydrocarbon products comprising:mixing said heavy hydrocarbon liquid feed with catalyst and hydrogen to form a heavy hydrocarbon slurry comprising hydrocarbon liquid and catalyst particles, said catalyst comprising molybdenum and carbon particles comprising pore volume of at least 0.2 cc/g, and a mean diameter of no more than 800 microns;hydrocracking hydrocarbons in said heavy hydrocarbon slurry in the presence of hydrogen and catalyst in a hydrocracking reactor to produce a hydrocracked slurry product comprising lighter hydrocarbon products; andwithdrawing said hydrocracked slurry product from said hydrocracking reactor.2. The process of wherein the molybdenum is impregnated on the carbon particles.3. The process of wherein the molybdenum is provided as molybdenum sulfide in the hydrocracking reactor.4. The process of wherein the molybdenum in the catalyst is no more than about 200 wppm in the feed.5. The process of wherein the carbon particles have a mean diameter of no more than 150 microns.6. The process of wherein the micropore volume of the carbon particles is less than 0.5 cc/g.7. The process of wherein the BET surface area of the carbon particles is at least 200 m/g.8. The process of wherein the carbon particles comprise no more than 2 wt % in the feed.9. The process of wherein the molybdenum is no more than about 175 wppm in the feed.10. The process of wherein the yield of TIOR in the product is no more than about 3.0 wt % of the feed.11. The process of wherein the yield of mesophase in the product is no more than ...

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Номер записи: 96
08-02-2018 дата публикации

Method for On-line Imaging of Mesophase Particles

Номер: US20180037827A1
Автор: Kellomaki Markku
Принадлежит:

On-line detection of mesophase particles employs a laser diode light source to illuminate a target area with a pulsed laser linearly or circularly polarized probe beam. Analysis of images determines extent of presence the birefringent mesophase particles, which are precursors to coking in catalytic hydrocracking processes. The inherently polarized low-coherence, unfocused but sufficiently collimated, pulsed laser beam yield sharp imaging with high depth of field of very small mesophase particles that are present in a moving, dark reactor liquid environment. 1. An on-line method for detection of mesophase particles formed in a hydrocarbon conversion reactor that comprises the steps of:(a) establishing a continuous reactor fluid stream containing mesophase particles;(b) employing a laser diode light source to illuminate a target area of the reactor fluid stream with a pulsed laser probe beam along a first beam path that comprises linearly polarized light or circularly polarized light such that an output beam emerges from the target area along a second beam path;(c) obtaining an image of the mesophase particles in the continuous reactor fluid stream; and(d) analyzing the image to determine at least one of (i) volume fraction or (ii) size distribution of mesophase particles in the continuous reactor fluid stream.2. The method of wherein the laser diode light source generates a pulsed laser probe beam without employing a polarizer filter.3. The method of wherein the probe beam is reflected from the target area to form the output beam.4. The method of wherein the probe beam is transmitted through the target area to form the output beam.5. The method of wherein the laser diode light source comprises a plurality of laser bars wherein each laser bar comprises one or more laser diodes and wherein the laser bars each emit a laser beam that is multiplexed to form the pulsed laser probe beam.6. The method of wherein each laser bar emits light of a different wavelength.7. The ...

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Номер записи: 97
08-02-2018 дата публикации

PRODUCTION OF UPGRADED PETROLEUM BY SUPERCRITICAL WATER

Номер: US20180037828A1
Автор: Alshareef Ali H., Choi Ki-Hyouk, Garhoush Mohammad S., LEE Joo-Hyeong
Принадлежит:

A method for upgrading a petroleum feedstock using a supercritical water petroleum upgrading system includes introducing the petroleum feedstock, water and an auxiliary feedstock. The method includes operating the system to combine the petroleum feedstock and the water to form a mixed petroleum feedstock and introducing separately and simultaneously into a lower portion of an upflowing supercritical water reactor. The auxiliary feedstock is introduced such that a portion of a fluid contained within the upflowing reactor located proximate to the bottom does not lack fluid momentum. An embodiment of the method includes operating the supercritical water petroleum upgrading system such that the upflowing reactor product fluid is introduced into an upper portion of a downflowing supercritical water reactor. The supercritical water petroleum upgrading system includes the upflowing supercritical water reactor and optionally a downflowing supercritical water reactor. 1. A method for upgrading a petroleum feedstock using a supercritical water petroleum upgrading system , the method comprising the steps of:introducing the petroleum feedstock into the supercritical water petroleum upgrading system;introducing a water into the supercritical water petroleum upgrading system; where the auxiliary feedstock comprises supercritical water,', 'where the auxiliary feedstock further comprises aromatic hydrocarbons from a naphtha reformer, where the aromatic hydrocarbons from a naphtha reformer are present in a range of from about 1 weight percent (wt. %) to about 75 wt. % of the auxiliary feedstock;, 'introducing an auxiliary feedstock into the supercritical water petroleum upgrading system,'}operating the supercritical water petroleum upgrading system such that the petroleum feedstock and the water combine to form a mixed petroleum feedstock;operating the supercritical water petroleum upgrading system such that the mixed petroleum feedstock and the auxiliary feedstock are introduced ...

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Номер записи: 98
12-02-2015 дата публикации

Hydrotreating process and apparatus relating thereto

Номер: US20150041365A1
Автор: David M. Bowman, Richard K. Hoehn, Soumendra Mohan Banerjee, Xin X. Zhu
Принадлежит: UOP LLC

One exemplary embodiment can be a process for treating a hydroprocessing fraction. The process can include obtaining a bottom stream from a fractionation zone, and passing at least a portion of the bottom stream to a film generating evaporator zone for separating a first stream containing less heavy polynuclear aromatic compounds than a second stream.

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Номер записи: 99
06-02-2020 дата публикации

MULTIPLE-BED CATALYTIC REACTOR COMPRISING A MIXING DEVICE

Номер: US20200038816A1
Автор: Brix Jacob, Holm-Christensen Olav, MANOHARAN Karthik Gopal, Risbjerg Jarlkov Klaus
Принадлежит: Haldor Topsoe A/S

The present invention relates to multi-bed catalytic reactor with a cylindrical shape comprising a mixing device mounted between two catalyst beds in the reactor, said mixing device has a circular outer rim which corresponds to the inner wall of the reactor, the mixing device comprises; collecting means disposed in a collecting section for collecting fluid from an up¬stream catalytic bed, mixing means disposed in a mixing section for mixing the collected fluid comprising guide vanes and guide ramps, and discharging means disposed in a discharging section for discharging the mixed fluid to a down-stream catalytic bed; wherein the collecting section, the mixing section and the discharging section are disposed outside the center of the circular cross-section of the reactor, as well as associated methods for mixing and the use of such a mixing device in catalytic reactors. 1. A multi-bed catalytic reactor with a cylindrical shape comprising a mixing device mounted between two catalyst beds in said reactor , said mixing device has a circular outer rim adapted to fit within the inner wall of the reactor , the mixing device comprises;collecting means disposed in a collecting section for collecting fluid from an up-stream catalytic bed,mixing means disposed in a mixing section comprising a floor, a ceiling and inner and outer walls for mixing the collected fluid, anddischarging means disposed in a discharging section for discharging the mixed fluid to a down-stream catalytic bed;wherein the mixing device has a donut shape and the collecting section, the mixing section and the discharging section are disposed outside the centre of the circular cross-section of the reactor and wherein said mixing means comprise guide vanes with a first and a second end, guide ramps with a first and a second end or comprises said guide vanes and said guide ramps.2. A multi-bed catalytic reactor with a cylindrical shape comprising a mixing device according to claim 1 , wherein the floor of said ...

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Номер записи: 100