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Небесная энциклопедия

Космические корабли и станции, автоматические КА и методы их проектирования, бортовые комплексы управления, системы и средства жизнеобеспечения, особенности технологии производства ракетно-космических систем

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Мониторинг СМИ

Мониторинг СМИ и социальных сетей. Сканирование интернета, новостных сайтов, специализированных контентных площадок на базе мессенджеров. Гибкие настройки фильтров и первоначальных источников.

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Поддерживает ввод нескольких поисковых фраз (по одной на строку). При поиске обеспечивает поддержку морфологии русского и английского языка
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Применить Всего найдено 7827. Отображено 100.
05-01-2012 дата публикации

Production of Low Color Middle Distillate Fuels

Номер: US20120000817A1
Автор: Stuart S. Shih
Принадлежит: ExxonMobil Research and Engineering Co

In a process for producing a low color diesel and/or kerosene fuel, a middle distillate feed can be supplied to a reactor having at least one first catalyst bed containing a first desulfurization and/or isomerization catalyst and at least one second catalyst bed containing a decolorization catalyst downstream from the first catalyst bed(s). The feed can be reacted with the hydrogen in the presence of the first catalyst at a temperature from about 290° C. to about 430° C. to produce a first liquid effluent, which can be cooled by about 10° C. to about 40° C. with a quench medium and cascaded to the at least one second catalyst bed. The cooled first liquid effluent can then be reacted with hydrogen in the presence of the decolorization catalyst at a temperature from about 280° C. to about 415° C. to produce a second effluent having an ASTM color less than 2.5.

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Номер записи: 1
12-01-2012 дата публикации

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

Номер: US20120009094A1
Автор: Roger K. Lott, Yu-Hwa Chang
Принадлежит: Individual

Systems for hydrocracking a heavy oil feedstock employ a colloidally or molecularly dispersed catalyst (e.g., molybdenum sulfide) which provide for concentration of the colloidally dispersed catalyst within the lower quality materials requiring additional hydrocracking. 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: 2
12-01-2012 дата публикации

Method and System for Synthesizing Liquid Hydrocarbon Compounds

Номер: US20120010304A1
Автор: Kazuhiko Tasaka
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 Engineering Co Ltd

Provided is a method for synthesizing liquid hydrocarbon compounds wherein synthesizing liquid hydrocarbon compounds from a synthesis gas by a Fisher-Tropsch synthesis reaction. The method includes a first absorption step of absorbing a carbon dioxide gas, which is contained in gaseous by-products generated in the Fisher-Tropsch synthesis reaction, with an absorbent, and a second absorption step of absorbing a carbon dioxide gas, which is contained in the synthesis gas, with the absorbent which is passed through the first absorption step.

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Номер записи: 3
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: 4
30-08-2012 дата публикации

Method for producing aviation fuel oil base and aviation fuel oil composition

Номер: US20120216449A1
Автор: Akira Koyama, Hideki Ono, Hideshi Iki, Kazuaki Hayasaka
Принадлежит: JX Nippon Oil and Energy Corp

A method for producing an aviation fuel oil base includes obtaining a first generated oil by hydrotreating a feedstock by bringing a feedstock which includes an oxygen-containing hydrocarbon compound derived from an animal or vegetable oils and fat into contact with a first dual functional catalyst which has dehydrogenation and hydrogenation functions and which includes a metal of group 6A of the periodic table, a metal of group 8, and an amorphous solid acidic substance, in the presence of hydrogen; and obtaining a second generated oil including an aviation fuel oil base by hydroisomerizing the first generated oil by bringing the first generated oil into contact with a second dual functional catalyst which has dehydrogenation and hydrogenation functions and which includes a metal of the group 8 of the periodic table and a crystalline solid acidic substance, in the presence of hydrogen.

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Номер записи: 5
04-10-2012 дата публикации

Fuels hydrocracking with dewaxing of fuel products

Номер: US20120248008A1
Автор: Michel Daage, Richard Dougherty, Stephen J. Mccarthy, Stuart S. Shih, William J. Novak
Принадлежит: ExxonMobil Research and Engineering Co

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.

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Номер записи: 6
04-10-2012 дата публикации

Apparatus for producing diesel

Номер: US20120251403A1
Автор: Andrew P. Wieber, Paul R. Zimmerman
Принадлежит: UOP LLC

An apparatus is disclosed for hydrocracking hydrocarbon feed in a hydrocracking unit and hydrotreating a diesel product from the hydrocracking unit in a hydrotreating unit. The hydrocracking unit and the hydrotreating unit shares the same recycle gas compressor. A warm separator separates recycle gas and hydrocarbons from diesel in the hydrotreating effluent, so fraction of the diesel is relatively simple. The warm separator also keeps the diesel product separate from the more sulfurous diesel in the hydrocracking effluent, and still retains heat needed for fractionation of lighter components from the low sulfur diesel product.

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Номер записи: 7
22-11-2012 дата публикации

Apparatus for hydroprocessing hydrocarbons

Номер: US20120294772A1
Автор: Andrew P. Wieber
Принадлежит: UOP LLC

An apparatus and process is disclosed for hydroprocessing hydrocarbon feed in a hydroprocessing unit and hydrotreating a second hydrocarbon. The hydrotreating effluent is mixed with hydroprocessing effluent and together fractionated.

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Номер записи: 8
14-03-2013 дата публикации

Hydrotreating of Aromatic-Extracted Hydrocarbon Streams

Номер: US20130062255A1
Автор: Omer Refa Koseoglu
Принадлежит: Saudi Arabian Oil Co

Deep desulfurization of hydrocarbon feeds containing undesired organosulfur compounds to produce a hydrocarbon product having low levels of sulfur, i.e., 15 ppmw or less of sulfur, is achieved by first subjecting the entire feed to an extraction zone to separate an aromatic-rich fraction containing a substantial amount of the aromatic refractory and sterically hindered sulfur-containing compounds and an aromatic-lean fraction containing a substantial amount of the labile sulfur-containing compounds. The aromatic-rich fraction is contacted with isomerization catalyst, and the isomerized aromatic-rich fraction and the aromatic-lean fraction are combined and contacted with a hydrotreating catalyst in a hydrodesulfurization reaction zone operating under mild conditions to reduce the quantity of organosulfur compounds to an ultra-low level.

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Номер записи: 9
14-03-2013 дата публикации

Integrated Isomerization and Hydrotreating Process

Номер: US20130062257A1
Автор: Omer Refa Koseoglu
Принадлежит: Saudi Arabian Oil Co

Deep desulfurization of hydrocarbon feeds containing undesired organosulfur compounds to produce a hydrocarbon product having low levels of sulfur, i.e., 15 ppmw or less of sulfur, is achieved by flashing the feed at a target cut point temperature to obtain two fractions. A low boiling temperature fraction contains refractory, sterically hindered sulfur-containing compounds, which have a boiling point at or above the target cut point temperature. A high boiling temperature fraction, having a boiling point below the target cut point temperature, is substantially free of refractory sulfur-containing compounds. The high boiling temperature fraction is contacted with isomerization catalyst, and the isomerized effluent and the low boiling temperature fraction are combined and contacted with a hydrotreating catalyst in a hydrodesulfurization reaction zone operating under mild conditions to reduce the quantity of organosulfur compounds to an ultra-low level.

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Номер записи: 10
21-03-2013 дата публикации

METHODS FOR INCREASING CATALYST CONCENTRATION IN HEAVY OIL AND/OR COAL RESID HYDROCRACKER

Номер: US20130068658A1
Автор: Chang Yu-Hwa, Lott Roger K.
Принадлежит: HEADWATERS TECHNOLOGY INNOVATION, LLC

Methods for hydrocracking a heavy hydrocarbon feedstock (e.g., heavy oil and/or coal resid) employ a catalyst composed of well dispersed metal sulfide catalyst particles (e.g., colloidally or molecularly dispersed catalyst particles, such as molybdenum sulfide), which provide an increased concentration of metal sulfide catalyst particles within lower quality materials requiring additional hydrocracking. In addition to increased metal sulfide catalyst concentration, the systems and methods provide increased reactor throughput, increased reaction rate, and higher conversion of asphaltenes and lower quality materials. Increased conversion of asphaltenes and lower quality materials also reduces equipment fouling, enables processing of a wider range of lower quality feedstocks, and leads to more efficient use of a supported catalyst if used in combination with the well dispersed metal sulfide catalyst particles. 1. A method of hydrocracking a heavy hydrocarbon feedstock using well dispersed metal sulfide catalyst particles , the method comprising:providing a heavy hydrocarbon feedstock that includes a significant fraction of hydrocarbons having a boiling point above 343° C. and/or asphaltenes;blending a catalyst precursor with the heavy hydrocarbon feedstock at a temperature below a decomposition temperature of the catalyst precursor to form a conditioned feedstock composition that is thereafter heated to above the decomposition temperature to form well dispersed metal sulfide catalyst particles in situ within the heavy hydrocarbon feedstock;{'sub': '2', 'introducing into a first hydrocracking reactor, hydrogen (H) gas and the heavy hydrocarbon feedstock including the well dispersed metal sulfide catalyst particles already formed in situ within the heavy hydrocarbon feedstock and/or the conditioned feedstock composition to form the well dispersed metal sulfide catalyst particles in situ within the heavy hydrocarbon feedstock when heated to above the decomposition ...

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Номер записи: 11
21-03-2013 дата публикации

PROCESS FOR THE SEQUENTIAL HYDROCONVERSION AND HYDRODESULFURIZATION OF WHOLE CRUDE OIL

Номер: US20130068661A1
Автор: Alzaid Ali Hussain, Hamad Esam Z., Kressmann Stephane Cyrille, SHAFI Raheel
Принадлежит: Saudi Arabian Oil Company

The invention relates to a method for removing sulfur from crude oils using a catalytic hydrotreating process operating at moderate temperature and pressure and reduced hydrogen consumption. The process produces sweet crude oil having a sulfur content of between about 0.1 and 1.0 wt % in addition to reduced crude density. The method employs least two reactors in series, wherein the first reactor includes a hydroconversion catalyst and the second reactor includes a desulfurization catalyst. 1. A method for upgrading crude oil , the method comprising:(a) contacting a crude oil feedstock with hydrogen gas to produce a hydrogen gas crude oil mixture;(b) contacting the hydrogen gas crude oil mixture with a hydroconversion catalyst in a first reactor maintained at a temperature of between about 400° C. and 450° C. to produce an effluent having an asphaltene content of less than 5% by weight, wherein said hydroconversion catalyst comprises a bimodal support material;(c) contacting the effluent from the first reactor with hydrogen gas to produce a effluent hydrogen gas mixture;(d) contacting the effluent hydrogen gas mixture with a desulfurization catalyst in a second reactor to produce an upgraded crude oil product having a reduced sulfur content and an increased API gravity, wherein said second reactor is maintained at a temperature that is less than the temperature that is maintained in the first reactor.2. The method of wherein the hydroconversion catalyst further comprises a base metal selected from the group consisting of a group VB metal claim 1 , a group VIB metal and a group VIIIB metal and wherein said bimodal support material comprises a first pore size having an average diameter of between about 6000 and 10000 Angstroms and a second pore size having an average diameter of between about 80 and 150 Angstroms.3. The method of wherein the hydroconversion catalyst further comprises a promoter metal claim 2 , wherein said promoter metal is selected from the group ...

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Номер записи: 12
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: 13
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: 14
11-04-2013 дата публикации

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

Номер: US20130087481A1
Автор: Heraud Jean-Philippe, Morel Frédéric, Quignard Alain
Принадлежит: IFP ENERGIES NOUVELLES

A process for the hydroconversion of heavy oil feedstocks comprises a step for hydroconversion of the feedstock in at least one reactor containing a catalyst in slurry mode used to recover metals from the residual unconverted fraction, especially those used as catalysts. The process comprises a hydroconversion step, a gas/liquid separation step, a liquid/liquid extraction step, a grinding step, a leaching step, a combustion step, a metals extraction step and a step for the preparation of catalytic solutions which are recycled to the hydroconversion step. 1. A process for the hydroconversion of heavy oil feedstocks containing metals , comprising:a. a step for hydroconversion of the feedstock in at least one reactor containing a catalyst in the form of a slurry containing at least one metal, and optionally a solid additive;b. a step for separation of the hydroconversion effluent without decompression into a fraction termed the light fraction containing compounds boiling at 500° C. at most and into a residual fraction;b′. an optional step for fractionation, comprising vacuum separation of said residual fraction as obtained in step b) to obtain a vacuum residue which is concentrated in metals;c. a step for liquid/liquid extraction of said residual fraction as obtained in step b) and/or said vacuum residue as obtained in step b′) using a solvent with a saturated nature in order to obtain a solid extract which is concentrated in metals and a raffinate;d. a step for grinding the solid extract which is concentrated in metals obtained from the liquid/liquid extraction step;e. a step for leaching the ground extract in the presence of water, a solvent with a saturated nature and a surfactant in order to obtain a solid extract and a leachate;f. a step for combustion of said solid extract obtained from the leaching step in the presence of oxygen in order to obtain ash which is concentrated in metals;g. a step for extraction of metals from the ash obtained in the combustion step; ...

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Номер записи: 15
18-04-2013 дата публикации

PRODUCTION OFLUBRICATING OIL BASESTOCKS

Номер: US20130092598A1
Автор: Carroll Michael Brian, DAAGE Michel, Dandekar Ajit Bhaskar, Hoo Teck-Mui, Joseck Eric D., Mentzer David
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Methods are provided for producing multiple lubricating oil basestocks from a feedstock. Prior to dewaxing, various fractions of the feedstock are exposed to hydrocracking conditions of different severity to produce a higher overall yield of basestocks. The hydrocracking conditions of different severity can represent exposing fractions of a feedstock to different processing conditions, exposing fractions of a feedstock to different amounts of hydrocracking catalyst, or a combination thereof. 1. A method for producing a plurality of basestocks , comprising:contacting a feedstock containing at least about 90 wt % of hydrocarbons boiling above 370° C. with a first hydrocracking catalyst under first effective hydrocracking conditions to produce a first hydrocracked effluent, the first hydrocracked effluent having a sulfur content of less than about 250 wppm, the first effective hydrocracking conditions being effective for conversion of about 5 wt % to about 30 wt % of the feedstock to hydrocarbons boiling below 370° C.;fractionating the first hydrocracked effluent to form a first hydrocracked fraction and a second hydrocracked fractioncontacting the first hydrocracked fraction with a second hydrocracking catalyst under second effective hydrocracking conditions to produce a third hydrocracked fraction, the third hydrocracked fraction having a viscosity index of at least about 100, the second effective hydrocracking conditions being effective for conversion of about 15 wt % to about 40 wt % of the first hydrocracked fraction to hydrocarbons boiling below 370° C.;contacting the second hydrocracked fraction with a third hydrocracking catalyst under third effective hydrocracking conditions to produce a fourth hydrocracked fraction, the fourth hydrocracked fraction having a viscosity index less than the viscosity index of the third hydrocracked fraction, the third effective hydrocracking conditions being effective for conversion of about 5 wt % to about 15 wt % of the second ...

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Номер записи: 16
25-04-2013 дата публикации

Hydrocracking process with interstage steam stripping

Номер: US20130098802A1
Автор: Ali H. Al-Abdul'al, Koji Nakano, Masaru Ushio, Omer Refa Koseoglu
Принадлежит: Individual

In a hydrocracking process, the product from the first stage reactor passes through a steam stripper to remove hydrogen, H 2 S, NH 3 , light gases (C 1 -C 4 ), naphtha and diesel products. The stripper bottoms are separated from hydrogen, H 2 S, NH 3 , light gases (C 1 -C 4 ), naphtha, and diesel products and treated in a second stage reactor. The effluent stream from the second stage reactor, along with the stream of separated hydrogen, H 2 S, NH 3 , light gases (C 1 -C 4 ), naphtha, and diesel products, are passed to a separation stage for separating petroleum fractions. Preferably, the effluent stream from the first stage reactor is passed through a steam generator prior to the steam stripping step. In an alternate embodiment, the effluent stream from the first stage reactor is passed through a vapor/liquid separator stripper vessel prior to the steam stripping step.

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Номер записи: 17
02-05-2013 дата публикации

SYNTHESIS OF A CRYSTALLINE SILICOALUMINOPHOSPHATE

Номер: US20130105360A1
Автор: Miller Stephen Joseph
Принадлежит:

The present invention is a method for synthesizing non-zeolitic molecular sieves which have a three dimensional microporous framework comprising [AlO] and [PO] units. In preparing the reaction mixture, a surfactant is used, coupled with non-aqueous impregnation to prevent acid sites from being destroyed by water during Pt impregnation. The superior SAPO exhibits higher activity and selectivity especially in catalytic hydroisomerization of waxy feeds, due to the presence of medium-sized silica islands distributed throughout the SAPO. 1. A hydrocarbon conversion process , comprising contacting a hydrocarbonaceous feed at hydrocarbon converting conditions with (hydrogen?) a catalyst comprising a silicoaluminophosphate molecular sieve having the Si MAS NMR spectrum of .2. The hydrocarbon conversion process of claim 1 , wherein the molecular sieve comprises a mean mesopore diameter of less than 200 angstroms.3. The hydrocarbon conversion process of claim 2 , wherein the molecular sieve comprises a mean mesopore diameter of less than 195 angstroms.4. The hydrocarbon conversion process of claim 3 , wherein the molecular sieve comprises a mean mesopore diameter of less than 190 angstroms.5. The hydrocarbon conversion process of claim 1 , wherein the silicoaluminophosphate molecular sieve has a three dimensional microporous framework structure of [AlO] and [PO] units wherein the ratio of Si atoms coordinated as Si(3Al1Si) to that coordinated as Si(4Si) claim 1 , as determined by Si MAS NMR claim 1 , is at least 0.5 claim 1 , the presence of Si atoms coordinated as Si(4Al) is less than 40 mol. %.6. The hydrocarbon conversion process of claim 1 , wherein the silicoaluminophosphate molecular sieve is selected from the group consisting of AEL claim 1 , ATO and AFO.7. The hydrocarbon conversion process of claim 1 , wherein the silicoaluminophosphate molecular sieve is AEL.8. The hydrocarbon conversion process of claim 1 , wherein the silicoaluminophosphate molecular sieve has a ...

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Номер записи: 18
09-05-2013 дата публикации

Production of low cloud point distillates

Номер: US20130112594A1
Автор: Berne K. Stober, Stuart S. Shih
Принадлежит: ExxonMobil Research and Engineering Co

Systems and methods are provided for producing at least one low sulfur distillate fuel product with improved low temperature properties. A potential distillate fuel feed is initially hydrotreated to reduce sulfur and nitrogen levels in the feed to desired amounts. The hydrotreated effluent is then fractionated to form several fractions, including a light diesel/distillate fraction and a heavy diesel fraction. The heavy diesel fraction is then dewaxed to improve the cold flow properties of the heavy diesel fraction. The dewaxed heavy diesel fraction can be combined with the light diesel fraction, or the dewaxed heavy diesel fraction can be fractionated as well. Optionally, the heavy diesel fraction is dewaxed under conditions effective for producing a dewaxed fraction with a cloud point that is less than or equal to the cloud point of the light diesel/distillate fraction.

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Номер записи: 19
09-05-2013 дата публикации

HYDROCRACKING PROCESS WITH INTEGRAL INTERMEDIATE HYDROGEN SEPARATION AND PURIFICATION

Номер: US20130112595A1
Автор: Al-Abdulal Ali Hasan, Mehra Yuv Raj, Ramaseshan Vinod
Принадлежит: Saudi Arabian Oil Company

An intermediate hydrogen separation and absorption-based purification system is integrated with a hydrocracking process for the production of relatively lower molecular weight products from a relatively heavy feedstock including sulfur-containing and nitrogen-containing hydrocarbon compounds. The integrated process allows the processing of heavy hydrocarbon feedstock having high nitrogen and high sulfur contents in a single-stage configuration and the using of noble metal catalyst in the hydrocracking reaction zone. The integrated process increases the overall catalytic activity and hydrogenation capability to produce superior distillate products. 1. An integrated hydrocracking process comprising:a. hydrotreating a feedstock with a hydrotreating catalyst in the presence of hydrogen to produce a hydrotreated effluent containing a reduced amount of sulfur-containing and/or nitrogen-containing hydrocarbon compounds as compared to the feedstock;b. separating the hydrotreated effluent in a high-pressure separation zone to produce a vapor stream and a hydrocarbon liquid stream;c. purifying at least a portion of the vapor stream in an absorption zone in the presence of at least a portion of relatively heavy components of the vapor stream from step (b) to produce a high purity hydrogen gas stream and a fuel gas stream;d. hydrocracking at least a portion of the hydrocarbon liquid stream from step (b) with a hydrocracking catalyst in the presence of hydrogen gas to produce a hydrocracked effluent, wherein the hydrogen gas includes at least a portion of the high purity hydrogen gas stream from step (c); ande. separating and fractionating the hydrocracked effluent to produce hydrocracked gas product and one or more hydrocracked liquid fractions.2. The process as in claim 1 , where step (b) comprises separating the hydrotreated effluent in a hot high-pressure separation zone to produce a hydrotreated gas stream and a hydrotreated liquid stream claim 1 , and separating the ...

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Номер записи: 20
09-05-2013 дата публикации

HYDROTREATING AND AROMATIC SATURATION PROCESS WITH INTEGRAL INTERMEDIATE HYDROGEN SEPARATION AND PURIFICATION

Номер: US20130112596A1
Автор: Al-Abdulal Ali Hasan, Mehra Yuv Raj, Ramaseshan Vinod
Принадлежит: Saudi Arabian Oil Company

An intermediate hydrogen separation and purification system is integrated with a hydrotreating and an aromatic saturation process for the production of relatively lower molecular weight products from a relatively heavy feedstock including sulfur-containing and aromatic-containing hydrocarbon compounds. The integrated process allows the processing of heavy hydrocarbon feedstock having high aromatic and high sulfur contents in a single-stage configuration and the using of noble metal catalyst in the aromatic saturation zone. The integrated process increases the overall catalytic activity and hydrogenation capability to produce superior distillate products. 1. An integrated hydroprocessing process for the production of relatively lower molecular weight products from a relatively heavy feedstock including sulfur-containing and aromatic-containing hydrocarbon compounds , the process comprising:a. hydrotreating the feedstock with a hydrotreating catalyst in the presence of hydrogen to produce a hydrotreated effluent containing a reduced amount of sulfur-containing hydrocarbon compounds;b. separating the hydrotreated effluent in a high-pressure separation zone to produce a vapor stream and a hydrocarbon liquid stream;c. purifying at least a portion of the vapor stream in an absorption zone in the presence of at least a portion of relatively heavier components of vapor stream from step (b) to produce a high purity hydrogen gas stream and a fuel gas stream;d. saturating the aromatic compounds contained in a portion of the hydrocarbon liquid stream with an aromatic saturation catalyst in the presence of hydrogen gas to produce an aromatic saturated effluent, wherein the hydrogen gas includes the high purity hydrogen gas stream from step (c) along with make-up hydrogen stream; ande. separating and fractioning the aromatic saturated effluent to produce one or more overhead gas streams, one or more sour water streams and overhead and bottom fractioned distillate products.2. The ...

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Номер записи: 21
16-05-2013 дата публикации

Pretreatment of fcc naphthas and selective hydrotreating

Номер: US20130118952A1
Автор: John Peter Greeley, Rohit Garg, Timothy Lee Hilbert, William Joseph Novak
Принадлежит: ExxonMobil Research and Engineering Co

This invention provides methods for multi-stage hydroprocessing treatment of FCC naphthas for improving the overall production quantity of naphtha boiling-range materials during naphtha production for low sulfur gasolines. Of particular benefit of the present processes is the selective treating of cat naphthas to remove gums instead of undercutting the overall naphtha pool by lowering the end cutpoints of the cat naphtha fraction. This maximizes the amount of refinery cat naphtha that can be directed to the gasoline blending pool while eliminating existing processing problems in hydrodesulfurization units. The processes disclosed herein have the additional benefit of minimizing octane losses in the increased naphtha pool volume.

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Номер записи: 22
06-06-2013 дата публикации

Method for producing hydrocarbon oil and system for producing hydrocarbon oil

Номер: US20130144099A1
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 (FT) synthesis reaction using a catalyst within a slurry bed reactor is fractionated into a distilled oil and a column bottom oil in a rectifying column, part of the column bottom oil is flowed into a first transfer line that connects a column bottom of the rectifying column to a hydrocracker, at least part of the column bottom oil is flowed into a second transfer line branched from the first transfer line and connected to the first transfer line downstream of the branching point, the amount of the catalyst fine powder to be captured is monitored while the catalyst fine powder in the column bottom oil that flows in the second transfer line are captured by a detachable filter provided in the second transfer line, and the column bottom oil is hydrocracked within the hydrocracker.

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Номер записи: 23
13-06-2013 дата публикации

HYDROCONVERSION PROCESS FOR HEAVY HYDROCARBONACEOUS FEEDSTOCK

Номер: US20130150637A1
Автор: Borremans Didier, Lacroix Maxime, Le Lannic-Dromard Katell, Ropars Marie, Vendrell Gloria
Принадлежит: TOTAL RAFFINAGE MARKETING

The invention concerns a process for hydroconversion of a hydrocarbonaceous feedstock comprising: 1. Process for the hydroconversion of a hydrocarbonaceous feedstock with an atomic H/C ratio of at least 0.25 , in the presence of hydrogen and at least one catalyst in at least one reactor , said process comprising a reaction step performed in a reaction section comprising at least one reactor and a separation step performed in a separation section , characterised in that it comprises: (i) at least one preparation reactor feeds one or more reactor of the reaction section, or', '(ii) each preparation reactor is dedicated for catalysts fed to at least a hydroconversion reactor or at least a hydrotreatment reactor of the reaction section;, 'a step of preparation of at least one catalyst in one or more preparation reactor upstream from the reaction section, wherein'}a step of separation of the solids contained in the liquid effluents issued from the reaction section, said step being performed in a liquid/solid separation apparatus of the separation section,a step of treatment of the residues issued from the separation section, comprising a partial oxidation step performed in a partial oxidation section wherein said residues are partially oxidized to produce carbon monoxide, hydrogen and a metal containing residue.2. Process according to claim 1 , wherein the hydrocarbonaceous feedstock is mixed with the catalyst precursor in the preparation reactors.3. Process according to claim 1 , wherein each catalyst is prepared in at least two preparation reactors.4. Process according to claim 1 , wherein each catalyst contained in a preparation reactor is dedicated to hydroconversion or hydrotreatment of said feedstock.5. Process according to claim 4 , wherein catalyst(s) dedicated to hydroconversion contain one transition metal selected from group VB claim 4 , VIB claim 4 , VIII claim 4 , in an active state claim 4 , and catalyst(s) dedicated to hydrotreatment contain two transition ...

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Номер записи: 24
20-06-2013 дата публикации

SATURATION PROCESS FOR MAKING LUBRICANT BASE OILS

Номер: US20130158314A1
Автор: Calla Jason Thomas, Schleicher Gary Paul
Принадлежит: EXXONMOBIL RESEARCH & ENGINEERING COMPANY

Systems and methods are provided for hydroprocessing a petroleum fraction, such as a bottoms fraction from a fuels hydrocracking process, to generate a lubricant base oil. A fuels hydrocracking process typically has less stringent requirements for the sulfur and nitrogen content of a feed as compared to a lubricant base oil. Additionally, depending on the nature of the feed for the fuels hydrocracking process, the bottoms fraction may contain a relatively high level of aromatics compounds. The aromatic content of such a petroleum fraction can be reduced using a aromatic saturation stage with multiple catalyst beds, or alternatively using a reactor (or reactors) with multiple aromatic saturation stages. The catalysts in the various beds or stages can be selected to provide different types of aromatic saturation activity. An initial bed or stage can provide activity for saturation of 1-ring aromatics in the petroleum fraction. One or more subsequent beds or stages, operating at successively lower temperature, can then be used to reduce the multiple-ring aromatic content of the petroleum fraction. 1. A method for producing a lubricant base oil , comprising:contacting an input feed having an aromatics content of at least 600 mmol/kg with a first catalyst under first effective aromatic saturation conditions to produce a first effluent containing less than 600 mmol/kg of aromatics, the first effective aromatic saturation conditions including a temperature of at least 300° C.;contacting the first effluent with a second catalyst under second effective aromatic saturation conditions to produce a second effluent, the second effective aromatic saturation conditions including a temperature of from 270° C. to 300° C. and a hydrogen partial pressure of at least 4.1 MPag (600 psig); andcontacting the second effluent with a third catalyst under third effective aromatic saturation conditions, the third effective aromatic saturation conditions including a temperature of from 220° C. ...

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Номер записи: 25
27-06-2013 дата публикации

METHOD FOR PRODUCING RENEWABLE FUELS

Номер: US20130161235A1
Автор: Foody Brian
Принадлежит: IOGEN BIO-PRODUCTS CORPORATION

According to the present invention, organic material is converted to biogas through anaerobic digestion and the biogas is purified to yield a combustible fluid feedstock comprising methane. A fuel production facility utilizes or arranges to utilize combustible fluid feedstock to generate renewable hydrogen that is used to hydrogenate crude oil derived hydrocarbons in a process to make liquid transportation or heating fuel. The renewable hydrogen is added to a reactor operated so as to simultaneously desulfurize and hydrogenate crude oil derived hydrocarbons. 1. A method of transforming waste organic material to produce a liquid transportation or heating fuel comprising:(a) subjecting waste organic material to anaerobic digestion by microorganisms in a biogas production facility that incorporates apparatus to collect the microbially generated biogas;(b) collecting an amount of crude biogas from the biogas production facility;(c) removing impurities from the crude biogas to yield a combustible fluid feedstock;(d) introducing a first amount of the combustible fluid feedstock from step (b) or (c) to apparatus for delivering a combustible fluid feedstock to fuel production facility;(e) withdrawing for use at a fuel production facility a second amount of combustible fluid feedstock approximately equal in energy content to the first amount of combustible fluid feedstock;(f) processing at the fuel production facility the second amount of combustible fluid feedstock to produce a third amount of renewable hydrogen; and(g) producing a fourth amount of liquid transportation or heating fuel by a process that comprises combining the third amount of renewable hydrogen derived from the second amount of combustible fluid feedstock with a crude oil derived liquid hydrocarbon and an additional effective amount of hydrogen of sufficient quantity to desulfurize the crude oil derived liquid hydrocarbon,wherein step (g) is carried out in a reactor under conditions to simultaneously ...

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Номер записи: 26
27-06-2013 дата публикации

INTEGRATED CRUDE REFINING WITH REDUCED COKE FORMATION

Номер: US20130161236A1
Автор: Brown Stephen Harold, Ceulemans Stefan Maria Willy, Stratton Donald E., Strauss Ramon A.
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Methods are provided for processing crude oil feeds with reduced or minimized energy usage, reduced or minimized numbers of processing steps, improved allocation of hydrogen, and reduced or minimized formation of low value products. The methods reduce or minimize the use of vacuum distillation, and in many aspects reduce or minimize the use of both atmospheric and vacuum distillation. The methods also reduce or minimize the use of coking and fluid catalytic cracking processes. 1. A method for processing a crude oil , comprising:separating a crude oil feedstock to form at least a naphtha fraction and a heavier crude oil fraction, a first cut point temperature for separating a lighter crude oil fraction comprising the naphtha fraction from the heavier crude oil fraction being a temperature from about 250° F. (121° C.) to about 400° F. (204° C.), the heavier crude oil fraction including a portion having a boiling point greater than 1050° F. (566° C.);hydrotreating the naphtha fraction under effective naphtha hydrotreating conditions to form a hydrotreated naphtha effluent;exposing the heavier crude oil fraction to a hydroconversion catalyst under effective hydroconversion conditions to form a hydroconverted effluent, the effective hydroconversion conditions being effective for conversion of at least about 30 wt % of the portion of the heavier crude oil having a boiling point greater than 1050° F. (566° C.);separating the hydroconverted effluent to form at least a distillate fraction and a bottoms fraction, a second cut point temperature for separating the distillate fraction from the bottoms fraction being a temperature from about 650° F. (343° C.) to about 800° F. (427° C.); andhydrotreating the distillate fraction under effective hydrotreating conditions to form a hydrotreated distillate effluent.2. The method of claim 1 , wherein separating the crude oil feedstock to form at least a naphtha fraction and a heavier crude oil fraction comprises separating the crude oil ...

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Номер записи: 27
25-07-2013 дата публикации

SELECTIVE MIDDLE DISTILLATE HYDROTREATING PROCESS

Номер: US20130186805A1
Автор: AL-BASSAM Abdulrahman, KOSEOGLU Omer Refa
Принадлежит:

A selective mid-distillate hydrotreating process is provided for production of hydrocarbon fuels with an ultra-low level of sulfur in which the initial hydrocarbon feedstock is introduced into to an aromatic extraction zone to produce an aromatic-lean fraction and an aromatic-rich fraction, which contain different classes of organosulfur compounds having different reactivities when subjected to hydrotreating reactions. The aromatic-lean fraction contains primarily labile heteroatom-containing compounds, and is passed to a first hydrotreating zone operating under mild conditions to remove the sulfur heteroatom from organosulfur hydrocarbon compounds. The aromatic-rich fraction contains primarily refractory heteroatom-containing compounds, including aromatic molecules such as certain benzothiophenes (e.g., long chain alkylated benzothiophenes), dibenzothiophene and alkyl derivatives, such as sterically hindered 4,6-dimethyldibenzothiophene, and is passed to a hydrotreating zone operating under relatively severe conditions to remove the heteroatom from sterically hindered refractory compounds. 1. A method of processing a hydrocarbon feed to reduce the concentration of undesired organosulfur compounds comprising:separating the hydrocarbon feed into an aromatic-lean fraction that contains labile heteroatom-containing compounds and an aromatic-rich fraction that contains refractory aromatic heteroatom-containing compounds;introducing the aromatic-lean fraction to a first hydrotreating zone operating at mild hydrotreating conditions effective for reducing the sulfur content of the aromatic-lean fraction and recovering a first hydrotreated effluent; andintroducing the aromatic-rich fraction to a second hydrotreating zone operating at conditions effective for reducing the sulfur content of the aromatic-rich fraction and recovering a second hydrotreated effluent.2. The method of claim 1 , further comprising:removing light gases from the second hydrotreated effluent to produce ...

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Номер записи: 28
01-08-2013 дата публикации

CATALYST PREPARATION REACTORS FROM CATALYST PRECURSOR USED FOR FEEDING REACTORS TO UPGRADE HEAVY HYDROCARBONACEOUS FEEDSTOCKS

Номер: US20130193035A1
Автор: Borremans Didier, Lacroix Maxime, Le Lannic-Dromard Katell, Vendrell Gloria
Принадлежит: TOTAL RAFFINAGE MARKETING

A process for upgrading heavy hydrocarbonaceous feedstocks in at least one hydroconversion reactor for hydroconversion of the heavy hydrocarbonaceous feedstocks and in at least one hydrotreatment reactor for hydrotreatment of the heavy hydrocarbonaceous feedstocks, comprising the preparation of two or more catalysts, each catalyst being prepared from one or more catalyst precursor in at least one specific preparation reactor, the catalyst precursor containing at least one transition metal selected from group IIA, IIIB, IVB, VB, VIB, VIIB, VIII, IB or IIB of the periodic table of elements, and each preparation reactor feeding one or more hydroconversion or hydrotreatment reactor, each catalyst contained in preparation reactors being dedicated to hydroconversion or hydrotreatment of the feedstocks. 1. Process for upgrading a heavy hydrocarbonaceous feedstock in at least one hydroconversion reactor for hydroconversion of said heavy hydrocarbonaceous feedstocks and in at least one hydrotreatment reactor for hydrotreatment of said heavy hydrocarbonaceous feedstocks , said process comprising the preparation of two or more catalysts , each catalyst being prepared from one or more catalyst precursor in at least one specific preparation reactor , said catalyst precursor containing at least one transition metal selected from group IIA , IIIB , IVB , VB , VIB , VIIB , VIII , IB or IIB of the periodic table of elements , and each preparation reactor feeding one or more hydroconversion or hydrotreatment reactor , each catalyst contained in a preparation reactor being dedicated to hydroconversion or hydrotreatment of said feedstock.2. Process according to claim 1 , wherein each preparation reactor is fed with a part of the feedstock to upgrade.3. Process according to claim 1 , wherein each preparation reactor is fed with a sulfiding agent.4. Process according to any of claim 1 , wherein each preparation reactor is fed with hydrogen.5. Process according to any of claim 1 , wherein ...

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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
12-09-2013 дата публикации

METHOD FOR UPGRADING EBBULATED BED REACTOR AND UPGRADED EBBULATED BED REACTOR

Номер: US20130233765A1
Автор: Lee Lap Keung, Lott Roger K.
Принадлежит:

A hydrocracking system is upgraded by modifying an existing ebullated bed initially utilizing a supported ebullated bed catalyst to thereafter utilize a dual catalyst system that includes metal sulfide catalyst particles and supported ebullated bed catalyst. The upgraded hydrocracking system achieves at least one of: (1) hydroprocess lower quality heavy oil; (2) increase conversion of higher boiling hydrocarbons that boil at 524° C. (975° F.) or higher; (3) reduce the concentration of supported ebullated bed catalyst required to operate an ebullated bed reactor at a given conversion level; and/or (4) proportionally convert the asphaltene fraction in heavy oil at the same conversion level as the heavy oil as a whole. The metal sulfide catalyst may include colloidal or molecular catalyst particles less than 1 micron in size and formed in situ within the heavy oil using a catalyst precursor well-mixed within the heavy oil and decomposed to form catalyst particles. 1. A method of upgrading a heavy oil hydroprocessing system to hydroprocess lower quality heavy oil having one or more of higher molecular weight , lower hydrogen-to-carbon ratio , or increased asphaltene concentration , comprising:initially operating an existing ebullated bed reactor using a supported ebullated bed catalyst to hydroprocess an initial heavy oil of a quality defined by at least one of molecular weight, hydrogen-to-carbon ratio, or asphaltene concentration;thereafter upgrading the existing ebullated bed reactor to operate using a dual catalyst system comprised of metal sulfide catalyst particles and supported ebullated bed catalyst; andoperating the upgraded ebullated bed reactor using the dual catalyst system to hydroprocess a lower quality heavy oil having one or more of higher molecular weight, lower hydrogen-to-carbon ratio, or higher asphaltene concentration compared to the initial heavy oil.2. A method as in claim 1 , wherein the lower quality heavy oil has a higher boiling point and a ...

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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
17-10-2013 дата публикации

PRODUCTION OF MIDDLE DISTILLATES FROM AN EFFLUENT ORIGINATING FROM FISCHER-TROPSCH SYNTHESIS COMPRISING A STEP OF REDUCING THE CONTENT OF OXYGENATED COMPOUNDS

Номер: US20130270153A1
Автор: BOUCHY Christophe, CALEMMA Vincenzo, DULOT Hugues, GREZAUD Aline, Heraud Jean-Philippe
Принадлежит:

Production of middle distillates from a feedstock produced by Fischer-Tropsch synthesis and containing oxygenated compounds: 2. Method according to in which said methanation step e) is subjected beforehand to a step f) of removal of water.3. Method according to in which said feedstock produced by Fischer-Tropsch synthesis comprises a content of n-paraffins greater than 60% by weight relative to the total weight of said feedstock claim 1 , a content of oxygenated compounds less than 10% by weight claim 1 , a content of unsaturated compounds less than 20% by weight and a content of iso-paraffins less than 10% by weight relative to the total weight of said feedstock.4. Method according to in which the catalyst used in step a) comprises at least one hydrogenating-dehydrogenating metal selected from the group comprising the metals of group VIB and of group VIII of the periodic table.5. Method according to in which step a) is carried out at a temperature comprised between 100 and 450° C. claim 1 , at a pressure comprised between 0.2 and 15 MPa claim 1 , the recycle hydrogen being fed into said hydrotreating step at a flow rate such that the hydrogen/feedstock volume ratio is comprised between 10 and 3000 normal litres per litre claim 1 , and at a hourly space velocity comprised between 0.1 and 40 h.6. Method according to in which step b) is carried out at a temperature comprised between 250 and 450° C. claim 1 , at a pressure comprised between 0.2 and 15 MPa claim 1 , at a space velocity comprised between 0.1 hand 10 h claim 1 , and at a hydrogen rate comprised between 100 and 2000 normal litres of hydrogen per litre of feedstock.7. Method according to in which claim 1 , when step e) is implemented on the liquid and gaseous effluent from the hydrotreating step a) claim 1 , said step e) is implemented in the presence of a methanation catalyst at a temperature comprised between 100 and 450° C. claim 1 , at a pressure comprised between 0.2 and 15 MPa claim 1 , at a space ...

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Номер записи: 33
17-10-2013 дата публикации

OPTIMIZED METHOD FOR PRODUCING MIDDLE DISTILLATES FROM A FEEDSTOCK ORIGINATING FROM THE FISCHER-TROPSCH PROCESS CONTAINING A LIMITED QUANTITY OF OXYGENATED COMPOUNDS

Номер: US20130270154A1
Автор: BOUCHY Christophe, CALEMMA Vincenzo, DULOT Hugues, GREZAUD Aline, HERAUD Jean Philippe
Принадлежит:

A method for producing middle distillates from a feedstock produced by Fischer-Tropsch synthesis and containing oxygenated compounds, including: 2. Method according to in which said feedstock produced by Fischer-Tropsch synthesis comprises a content of n-paraffins greater than 60% by weight relative to the total 2 PET-2854 weight of said feedstock claim 1 , a content of oxygenated compounds less than 10% by weight claim 1 , a content of unsaturated compounds less than 20% by weight and a content of iso-paraffins less than 10% by weight relative to the total weight of said feedstock.3. Method according to in which the catalyst used in step a) comprises at least one hydrogenating-dehydrogenating metal selected from the group comprising the metals of group VIB and of group VIII of the periodic table on a support.4. Method according to in which the catalyst used in step a) comprises at least one group VIII non-noble metal selected from nickel and cobalt in combination with at least one group VIB metal selected from molybdenum and tungsten claim 3 , used alone or in a mixture.5. Method according to in which the support of the catalyst used in step a) is a support based on alumina.6. Method according to in which the support of the catalyst used in step a) is a support based on alumina containing a group VIII metal selected from nickel or cobalt.7. Method according to in which the catalyst used in step a) has a BET specific surface area from 100 to 300 m/g claim 1 , a mean mesopore diameter comprised between 6 and 20 nm claim 1 , a pore volume of the pores the diameter of which is comprised between the average diameter as defined above reduced by 3 nm and the average diameter as defined above increased by 3 nm greater than 20% of the total pore volume claim 1 , a total pore volume comprised between 0.1 and 1 ml/g.8. Method according to in which the catalyst used in step a) is used in reduced form.9. Method according to in which step a) is carried out at a temperature ...

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Номер записи: 34
24-10-2013 дата публикации

PROCESS FOR THE REFINING OF CRUDE OIL

Номер: US20130277274A1
Автор: Bellussi Giuseppe, Rispoli Giacomo Fernando
Принадлежит: ENI S.P.A.

A process for the refining of crude oil, comprising a separation unit of the crude oil, consisting of at least one atmospheric distillation unit for separating the various fractions, a unit for the conversion of the heavy fractions obtained, a unit for improving the quality of some of the fractions obtained by actions on the chemical composition of their constituents, and units for the removal of undesired components, characterized in that the heaviest fraction, the atmospheric distillation residue, is sent to the conversion unit comprising a hydroconversion reactor in slurry phase or of the ebullated bed type, into which hydrogen or a mixture of hydrogen and ¾S is introduced in the presence of a suitable nanodispersed hydrogenation catalyst. 1. A process for refining crude oil , comprising a separation unit of the crude oil , consisting of at least one atmospheric distillation unit for separating the various fractions , units for the conversion of the heavy fractions obtained , units for improving the quality of some of the fractions obtained by actions on the chemical composition of their constituents , and units for the removal of undesired components , characterized in that the heaviest fraction , the atmospheric distillation residue , is sent to the conversion unit comprising at least one hydroconversion reactor in slurry phase or of the ebullated bed type , wherein hydrogen or a mixture of hydrogen and HS is introduced in the presence of a suitable nanodispersed hydrogenation catalyst.2. The process according to claim 1 , wherein the nanodispersed hydrogenation catalyst is based on a sulfide of Mo and/or Fe and/or W and/or Cr and/or Ni and/or Co and mixtures thereof.3. The process according to claim 1 , wherein claim 1 , when the hydroconversion reactor is of the ebullated bed type claim 1 , a suitable heterogeneous claim 1 , supported hydroconversion co-catalyst is also present.4. The process according to claim 1 , wherein claim 1 , when the hydroconversion ...

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Номер записи: 35
07-11-2013 дата публикации

INTEGRATED EBULLATED-BED PROCESS FOR WHOLE CRUDE OIL UPGRADING

Номер: US20130292299A1
Автор: KOSEOGLU Omer Refa, Ranc Alain Paul
Принадлежит: Saudi Arabian Oil Company

A system and process for upgrading a whole crude oil feed in an integrated ebullated-bed and hydrotreater is provided in which the whole crude oil is flashed into a flashed straight run distillates fraction and an atmospheric residue fraction. The atmospheric residue fraction is hydroprocessed in an ebullated-bed reaction zone, while the flashed straight run distillates fraction and the products fraction produced from the ebullated-bed reaction zone are hydrotreated in a fixed-bed reaction zone. Distillates from the hydrotreater and the unconverted residue fraction from the ebullated-bed reaction zone can be combined to produce an upgraded synthetic crude oil. 1. A method for upgrading a crude oil feed to reduce the content of undesired heteroatom compounds containing metals , sulfur and nitrogen , the method comprising:a. heating the crude oil feed and flashing the heated crude oil feed to produce a flashed straight run distillate fraction and an atmospheric residue fraction;b. hydroprocessing the atmospheric residue fraction in an ebullated-bed reaction zone in the presence of hydrogen and an ebullated-bed reactor catalyst to produce an ebullated-bed reactor effluent stream, wherein make-up hydrogen is introduced as needed;c. separating the ebullated-bed reactor effluent stream into a hydroprocessed products stream containing hydrogen, a recycle oil stream and an unconverted residue stream;d. hydrotreating in a fixed bed hydroprocessing zone a combined stream of the hydroprocessed products stream containing hydrogen and the flashed straight run distillate fraction in the presence of a hydrotreating catalyst in a hydrotreater to produce a hydrotreated effluent, wherein hydrogen from the hydroprocessed products stream forms at least a portion of the requisite hydrogen for hydrotreating reactions;e. separating the hydrotreated effluents to produce a light gas stream and a hydrotreated distillate stream; andf. purifying the light gas stream and recycling the purified ...

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Номер записи: 36
21-11-2013 дата публикации

CATALYST AND PROCESS FOR HYDROCONVERSION OF A HEAVY FEEDSTOCK

Номер: US20130306517A1
Автор: KESTER John George, KOMAR David Andrew, SHERWOOD David Edward
Принадлежит:

A hydroconversion catalyst comprising a Group VIB metal component, a Group VIII metal component and a carrier material is disclosed wherein said catalyst has a total surface area of 240 to 360 m/g; a total pore volume of 0.5 to 0.9 cc/g; and a pore volume distribution such that greater than 60% of pore volume are in pores present as micropores of diameter between 55 and 115 Å, less than 0.12 cc/g of pore volume are in pores present at pores of diameter greater than 160 Å and less than 10% of pore volume are in pores present as macropores of diameters greater than 250 Å. 1. A hydroprocessing catalyst for treating heavy hydrocarbon feedstocks , wherein said catalyst comprises: a calcined particle comprising a co-mulled mixture made by co-mulling inorganic oxide powder or powders , solution or solutions containing molybdenum and Group VIII metals and optionally water , acid and flocculating agent , and then forming said co-mulled mixture into a particle that is calcined to thereby provide said calcined particle , said calcined particles having:{'sup': '2', 'a. a total surface area of 240 to 360 m/g;'}b. a total pore volume of 0.5 to 0.9 cc/g; andc. a pore volume distribution such that greater than 60% of pore volume are in pores present as micropores of diameter between 55 and 115 Å, less than 0.12 cc/g of pore volume are in pores present at pores of diameter greater than 160 Å and less than 10% of pore volume are in pores present as macropores of diameters greater than 250 Å.2. The catalyst of claim 1 , wherein said calcined particle has a shape comprising a first end claim 1 , a second end and a wall disposed between said ends claim 1 , said wall comprising 3 or 4 lobes formed in the length of the wall.3. The catalyst of claim 1 , wherein said inorganic oxide material is selected from the group consisting of alumina claim 1 , silica and alumina-silica.4. The catalyst of claim 1 , wherein said calcined mixture has a molybdenum content in the range of from 1 weight ...

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Номер записи: 37
21-11-2013 дата публикации

Coprocessing of biofeeds with group vi metal catalysts

Номер: US20130310618A1
Автор: Bradley R. Fingland, Patrick Loring Hanks
Принадлежит: ExxonMobil Research and Engineering Co

Feedstocks containing biocomponent materials are coprocessed with mineral feeds using a Group VI metal catalyst prior to hydrodesulfurization of the feedstocks. The Group VI metal catalyst is optionally a physically promoted Group VI metal catalyst.

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Номер записи: 38
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: 39
05-12-2013 дата публикации

METHOD FOR CONVERTING HYDROCARBON FEEDSTOCK COMPRISING A SHALE OIL BY HYDROCONVERSION IN AN EBULLATING BED, FRACTIONATION BY ATMOSPHERIC DISTILLATION AND HYDROCRACKING

Номер: US20130319908A1
Автор: Halais Christophe, Leroy Helene, Morel Frédéric, Plain Cecille
Принадлежит:

Method and plant for converting hydrocarbon feedstock comprising a shale oil, comprising a step of hydroconverting in an ebullating bed, a fractionation into a light fraction, a naphtha fraction, a gas-oil fraction and a fraction heavier than gas-oil, the naphtha and gas oil fraction being hydrotreated, the fraction heavier than gas oil being hydrocracked, the products of the hydrocracking being sent to the step for hydrotreating. The method aims to maximize the yield of fuel bases. 1. Method for converting a shale oil or a mixture of shale oils having a nitrogen content of at least 0.1% , comprising:a) the feedstock is conveyed into a section for hydroconverting in the presence of hydrogen, said section comprising at least one ebullating bed reactor operating in gas and liquid upflow mode and containing at least one supported hydroconversion catalyst,b) the effluent obtained in step a) is conveyed at least partly into a fractionating zone, from which, by atmospheric distillation, a gaseous fraction, a naphtha fraction, a gas-oil fraction and a fraction heavier than gas-oil are recovered,c) said naphtha fraction is treated at least partly in a first section for hydrotreating in the presence of hydrogen, said section comprising at least one fixed bed reactor containing at least one hydrotreating catalyst,d) said gas-oil fraction is treated at least partly in a second section for hydrotreating in the presence of hydrogen, said section comprising at least one fixed bed reactor containing at least one hydrotreating catalyst, ande) the fraction heavier than the gas-oil fraction is treated at least partly in a hydrocracking section in the presence of hydrogen.2. Method according to claim 1 , wherein the hydrocracking effluents obtained at the end of step e) are fractionated into a second gaseous fraction claim 1 , a second naphtha fraction claim 1 , a second gas-oil fraction claim 1 , and a second fraction which is heavier than gas-oil.3. Method according to claim 2 , ...

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Номер записи: 40
12-12-2013 дата публикации

METHOD FOR CONVERTING HYDROCARBON FEEDSTOCK COMPRISING A SHALE OIL BY DECONTAMINATION, HYDROCONVERSION IN AN EBULLATING BED, AND FRACTIONATION BY ATMOSPHERIC DISTILLATION

Номер: US20130327682A1
Автор: Halais Christophe, Leroy Helene, Morel Frédéric, Plain Cecile
Принадлежит:

Method and plant for converting hydrocarbon feedstock comprising a shale oil, comprising a step of decontaminating, a step of hydroconverting in an ebullating bed, a step of fractionating into a light fraction, a naphtha fraction, a gas-oil fraction and a fraction heavier than the gas-oil fraction, the naphtha and gas-oil fractions being hydrotreated, the fraction heavier than the gas-oil fraction being conveyed to the decontaminating step. The method aims to maximize the yield of fuel bases. 1. Method for converting a shale oil or a mixture of shale oils having a nitrogen content of at least 0.1% , often at least 1% and very often at least 2% by weight , characterized in that it comprises the following steps:a) The feedstock is subjected to a decontamination, to give a residue and a decontaminated oil,b) The decontaminated oil is conveyed to a section for hydroconverting in the presence of hydrogen, said section comprising at least one ebullating bed reactor operating in gas and liquid upflow mode and containing at least one supported hydroconverting catalyst,c) The effluent obtained in step b) is conveyed at least partly, and often entirely, into a fractionating zone, from which, by atmospheric distillation, a gaseous fraction, a naphtha fraction, a gas-oil fraction and a fraction heavier than gas-oil are recovered,d) Said naphtha fraction is treated at least partly, and often entirely, in another section for hydrotreating in the presence of hydrogen, said section comprising at least one fixed bed reactor containing at least one hydrotreating catalyst, ande) Said gas-oil fraction is treated at least partly, and often entirely, in a section for hydrotreating in the presence of hydrogen, said section comprising at least one fixed bed reactor containing at least one hydrotreating catalyst.2. Method according to claim 1 , characterized in that it further comprises a step f) claim 1 , in which at least a part of the fraction heavier than gas-oil is conveyed to step a) ...

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Номер записи: 41
19-12-2013 дата публикации

HYDRODESULFURIZATION, DEOXYGENATION AND DEWAXING PROCESSES WITH WATER STABLE CATALYSTS FOR BIOMASS-CONTAINING HYDROCARBON FEEDSTOCKS

Номер: US20130338414A1
Автор: Fingland Bradley R., Gatt Joseph E.
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

This invention relates to a method for hydroprocessing feedstreams containing both sulfur-containing mineral oils and biomass-derived feedstocks in a single reactor configuration. The process produces a desulfurized, deoxygenated and dewaxed hydrocarbon product having reduced oxygen content, increased iso-paraffin content, low n-paraffin content, and good cold flow properties. In preferred embodiments, the processes herein utilize water tolerant hydrodewaxing catalysts in order to prevent deactivation and/or catalyst loss due to water produced during the deoxygenation reactions in the biomass components. 1. A method for processing a hydrocarbon feedstock comprised of a mineral oil component and a biomass oil component to form at least one liquid motor fuel product , such method comprising:a) contacting the hydrocarbon feedstock and a first hydrogen treat gas stream with a hydrodesulfurization/deoxygenation catalyst in a first reaction zone of a hydroprocessing reactor under first hydroprocessing conditions sufficient to produce a first reaction zone effluent which contains less organically bound sulfur than the hydrocarbon feedstock and less organically bound oxygen than the hydrocarbon feedstock;b) contacting the first reaction zone effluent with a dewaxing catalyst in a second reaction zone of the hydroprocessing reactor under second hydroprocessing conditions sufficient to produce a second reaction zone effluent;c) separating a gas phase product stream from the second reaction zone effluent to produce a reactor effluent product which has a lower sulfur content and a lower oxygen content than the hydrocarbon feedstock; andd) producing at least one liquid motor fuel product from at least a portion of the reactor effluent product;wherein the dewaxing catalyst comprises a zeolitic support, at least one active metal compound comprising one or more of Group VIB metals and Group VIII metals deposited thereon, and a hydrophilic, hydrothermally-stable binder comprising ...

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Номер записи: 42
26-12-2013 дата публикации

HYDROCRACKING PROCESS SELECTIVE FOR IMPROVED DISTILLATE AND IMPROVED LUBE YIELD AND PROPERTIES

Номер: US20130341243A1
Автор: Bradway Robert Allen, DAAGE Michel, Hilbert Timothy Lee, Novak William J., Shih Stuart S.
Принадлежит: ExxonMobil Research and Engineering

This invention relates to a process involving hydrocracking of a feedstream in which a converted fraction can exhibit relatively high distillate product yields and maintained or improved distillate fuel properties, while an unconverted fraction can exhibit improved properties particularly useful in the lubricant area. In this hydrocracking process, it can be advantageous for the yield of converted/unconverted product for gasoline fuel application to be reduced or minimized, relative to converted distillate fuel and unconverted lubricant. Catalysts and conditions can be chosen to assist in attaining, or to optimize, desirable product yields and/or properties. 1. A hydrocracking process on a vacuum gasoil feedstream being selective for distillate boiling range converted products and yielding unconverted products useful as lubricants , which process comprises:providing a vacuum gasoil feedstream having a nitrogen content of not greater than about 50 wppm and a sulfur content of not greater than about 300 wppm;hydrocracking the vacuum gasoil feedstream in a high-conversion hydrocracking stage with a hydrogen-containing treat gas stream in the presence of a two-stage catalyst system under effective hydrocracking conditions sufficient to attain a conversion level of greater than 55%, so as to form a hydrocracked product; andseparating the hydrocracked product into a converted product having a boiling range maximum of about 700° F. (about 371° C.) and an unconverted product having a boiling range minimum of about 700° F. (about 371° C.), the converted product having one or more of a cetane number of at least 45, a smoke point of at least 20 mm, and a sulfur content of not greater than 12 wppm, the unconverted product having one or more of a viscosity index of at least 80, a pour point of less than 5° C., and a kinematic viscosity at about 100° C. of at least 1 cSt,wherein the two-stage catalyst system comprises (i) a USY catalyst containing a Group VIII noble metal ...

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Номер записи: 43
02-01-2014 дата публикации

METHOD FOR HYDROTREATING HEAVY HYDROCARBON FEEDSTOCKS USING PERMUTABLE REACTORS, INCLUDING AT LEAST ONE STEP OF SHORT-CIRCUITING A CATALYST BED

Номер: US20140001089A1
Автор: BAZER-BACHI Frederic, BOYER Christophe, Guibard Isabelle, Marchal Nicolas, Plain Cecile
Принадлежит: IFP ENERGIES NOUVELLES

Process for hydrotreating a heavy hydrocarbon fraction using a system of switchable fixed bed guard zones each containing at least two catalyst beds and in which whenever the catalyst bed that is brought initially into contact with the feed is deactivated and/or clogged during the steps in which the feed passes successively through all the guard zones, the point of introduction of the feed is shifted downstream. The present invention also relates to an installation for implementing this process. 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 conditions of hydrotreating , over a hydrotreating catalyst , in at least two fixed bed hydrotreating guard zones each containing at least two catalyst beds , 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 catalyst beds of the guard zones for a period at most equal to the deactivation time and/or clogging time of a guard zone,a step a′) during which the feed is introduced, by-passing the deactivated and/or clogged catalyst bed, onto the next catalyst bed not yet deactivated and/or clogged of the same guard zone for a period at most equal to the deactivation time and/or clogging time of a guard zone,step a′) being repeated until the feed is introduced onto the last catalyst bed not yet deactivated and/or clogged of the same guard zone for a period at most equal to the deactivation time and/or clogging time,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 catalyst beds of the guard zones, the ...

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Номер записи: 44
02-01-2014 дата публикации

PROCESS FOR HYDROTREATING HEAVY RAW OILS

Номер: US20140001090A1
Автор: DAI Lishun, HU Dawei, LI Dadong, Liu Jia, Liu Tao, LIU Xuefen, NIE Hong, Shao Zhicai, Sun Shuling, YANG Qinghe, Zhao Xinqiang
Принадлежит:

The present invention relates to a catalyst combination for hydrotreating raw oils and a process for hydrotreating raw oils with the catalyst combination. The catalyst combination comprises 1. A catalyst combination for hydrotreating raw oils , which comprisesone or both of at least one hydrogenation protection catalyst I and at least one hydrogenation demetalling catalyst I;at least one hydrogenation demetalling catalyst II; andat least one hydrogenation treatment catalyst III;wherein, the content of said hydrogenation demetalling catalyst II in said catalyst combination, by volume and based on the total volume of the catalyst combination, is 5-50%;wherein, said hydrogenation demetalling catalyst II has a support, which is a shaped alumina support,the support has a pore volume measured by the mercury porosimetry of 0.9-1.2 mL/g;{'sup': '2', 'the support has a specific surface area of 50-300 m/g;'}the support has a ratio of the volume of the pores having a diameter of 10 nm-30 nm to the total pore volume of 55-80%, preferably 55-72%, more preferably 59-66%;the support has a ratio of the volume of the pores having a diameter of 300 nm-500 nm to the total pore volume of 10-35%, preferably 18-35%, more preferably 26-32%.2. The catalyst combination of claim 1 , whereinthe catalyst combination comprises the hydrogenation protection catalyst I, the hydrogenation demetalling catalyst II and the hydrogenation treatment catalyst III, wherein by volume and based on the total volume of the catalyst combination, the content of the hydrogenation protection catalyst I is 5-60%, the content of the hydrogenation demetalling, catalyst II is 5-50%, and the content of the hydrogenation treatment catalyst III is 10-60%; the hydrogenation protection catalyst I has a bed voidage of 25-60%;orthe catalyst combination comprises the hydrogenation demetalling catalyst I, the hydrogenation demetalling catalyst II and the hydrogenation treatment catalyst III, wherein by volume and based on the ...

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Номер записи: 45
02-01-2014 дата публикации

CROSS FLOW GAS-LIQUID CATALYTIC REACTION SYSTEMS

Номер: US20140001095A1
Автор: Korsten Hans G.
Принадлежит:

A gas-liquid catalyzed reaction is performed by introducing at least a portion of the reactive gas into the catalyst as a cross-flow or radial-flow stream. Introducing at least a portion of the reactive gas as a radial flow stream allows the reactive gas to travel through the catalyst bed along a shorter path length. This reduces the pressure drop for the radial flow portion of the gas. The reactive gas can be introduced into the catalyst bed at various heights relative to the height of the catalyst bed. 1. A method for performing a catalyzed gas-liquid reaction , comprising:providing a first catalyst bed in a reactor, the reactor including an inner conduit that occupies a portion of the volume of the first catalyst bed and an outer gap between the first catalyst bed and a wall of the reactor, wherein the reactor further comprises a reactor effluent outlet which is fluidly connected to the first catalyst bed;exposing an axial flow of a hydrocarbon feedstock to a first catalyst located in the first catalyst bed in the presence of a reactive gas under effective processing conditions to produce a first liquid reaction effluent; anddelivering at least a portion of the reactive gas flow into the first catalyst bed via the inner conduit as a radial flow, thereby contacting the hydrocarbon feedstock and the first catalyst in the first catalyst bed under first effective processing conditions;wherein at least about 50 vol % of the reactive gas flow exits the first catalyst bed by passing into the outer gap, and at least 50 vol % of the first liquid reaction effluent exits the reactor via the reactor effluent outlet.2. The method of claim 1 , wherein the first effective processing conditions comprise effective hydroprocessing conditions and the reactive gas comprises hydrogen.3. The method of claim 1 , wherein passing at least about 50 vol % of the reactive gas flow into the outer gap comprises passing the at least about 50 vol % of the reactive gas flow through a gas/liquid ...

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Номер записи: 46
02-01-2014 дата публикации

Use of n-paraffin adsorption to increase selectivity and yield of synthetic distillate fuel

Номер: US20140005450A1
Автор: Charles P. Luebke, John A. Petri, Michael J. McCall, Terry L. Marker, Tom N. Kalnes
Принадлежит: UOP LLC

Methods of making synthetic distillate fuel are described. The methods involve the use of an absorbent bed of molecular sieves which adsorb the n-paraffins from a distillate fuel cut. This allows the distillate fuel true boiling point cut point on the distillation column to increase to a higher temperature to make a distillate fuel which meets all of the synthetic paraffinic kerosene (SPK) or synthetic diesel specifications on distillation as well as the cold flow property specification, such as freeze point for SPK or cloud point, cold filter plugging point and pour point for synthetic diesel. This approach could improve aviation fuel yields by about 5 to about 10% and synthetic diesel yields up to 20%.

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Номер записи: 47
30-01-2014 дата публикации

SPHERICAL MATERIAL COMPRISING METALLIC NANOPARTICLES TRAPPED IN A MESOSTRUCTURED OXIDE MATRIX AND ITS USE AS A CATALYST IN REFINING PROCESSES

Номер: US20140027346A1
Автор: Boissiere Cedric, Bonduelle Audrey, Chaumonnot Alexandra, Colbeau-Justin Frederic, Sanchez Clement
Принадлежит:

An inorganic material is described, constituted by at least two elementary spherical particles, each of said spherical particles comprising metallic nanoparticles having at least one band with a wave number in the range 750 to 1050 cmin Raman spectroscopy and containing one or more metals selected from vanadium, niobium, tantalum, molybdenum and tungsten, said metallic nanoparticles being trapped in a mesostructured matrix based on an oxide of an element Y selected from silicon, aluminium, titanium, tungsten, zirconium, gallium, germanium, tin, antimony, lead, vanadium, iron, manganese, hafnium, niobium, tantalum, yttrium, cerium, gadolinium, europium and neodymium. Said matrix has pores with a diameter in the range 1.5 to 50 nm and amorphous walls with a thickness in the range 1 to 30 nm. Said elementary spherical particles have a maximum diameter of 200 microns and said metallic nanoparticles have a maximum dimension strictly less than 1 nm. 1. An inorganic material constituted by at least two elementary spherical particles , each of said spherical particles comprising metallic nanoparticles having at least one band with a wave number in the range 750 to 1050 cmin Raman spectroscopy and containing at least one or more metals selected from vanadium , niobium , tantalum , molybdenum and tungsten , said metallic nanoparticles being present within a mesostructured matrix based on an oxide of at least one element Y selected from the group constituted by silicon , aluminium , titanium , tungsten , zirconium , gallium , germanium , tin , antimony , lead , vanadium , iron , manganese , hafnium , niobium , tantalum , yttrium , cerium , gadolinium , europium and neodymium and a mixture of at least two of these elements , said matrix having pores with a diameter in the range 1.5 to 50 nm and having amorphous walls with a thickness in the range 1 to 30 nm , said elementary spherical particles having a maximum diameter of 200 microns and said metallic nanoparticles having a ...

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Номер записи: 48
13-02-2014 дата публикации

CO-PRODUCTION OF HEAVY AND LIGHT BASE OILS

Номер: US20140042056A1
Автор: Calla Jason Thomas, DAAGE Michel, Dandekar Ajit Bhaskar, Prentice Krista Marie
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

A suitable feedstock for forming lubricant base oils is separated into at least a lower boiling portion and a higher boiling portion. The lower boiling portion is combined with a feed suitable for use as a fuels hydrocracking feed. The combined feed is hydrocracked and catalytically dewaxed in order to form fuels and Group II, Group II+, or Group III light neutral basestocks. The higher boiling portion of the feedstock is solvent processed in order to form Group I heavy neutral base oils and/or Group I brightstock base oils. The higher boiling portion of the feedstock can correspond to both a bottoms fraction and one or more additional fractions boiling above a fractionation cut point. 1. A method for forming fuel and lubricant products , comprising:separating a feedstock into at least a first fraction having a T5 boiling point greater than 600° F. (316° C.) and a T95 boiling point of 1150° F. (621° C.) or less and a bottoms fraction;deasphalting the bottoms fraction to form a deasphalted bottoms fraction and an asphalt product;extracting the deasphalted bottoms in the presence of an extraction solvent to form a raffinate stream and an extract stream, an aromatics content of the raffinate stream being lower than an aromatics content of the deasphalted bottoms;dewaxing the raffinate stream in the presence of a dewaxing solvent to form a lubricant base oil product and a wax product;hydroprocessing a combined feedstock corresponding to the first fraction and a fuels feedstock, at least a portion of the combined feedstock having a boiling point greater than 700° F. (371° C.), the fuels feedstock having a T5 boiling point greater than 350° F. (177° C.) and a T95 boiling point of 1150° F. (621° C.) or less, under first effective hydroprocessing conditions to form a hydroprocessed effluent;separating the hydroprocessed effluent to form at least a gas phase effluent and a liquid phase effluent;hydroprocessing at least a portion of the liquid phase effluent in the presence ...

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Номер записи: 49
20-02-2014 дата публикации

HYDROPROCESSING OF HIGH NITROGEN FEED USING BULK CATALYST

Номер: US20140048448A1
Автор: COLE Kathryn Y., Hanks Patrick L., Hilbert Timothy L., Novak William J.
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Methods are provided for hydrotreating high nitrogen feeds with improved results for nitrogen removal, aromatic saturation, and/or sulfur removal. The method includes hydrotreating the feed with a supported hydrotreating catalyst followed by a bulk metal catalyst, the hydrotreated effluent of which can be suitable for use as a feed to an FCC reactor. 1. A method for effectively utilizing heteroatom removal capability of a bulk catalyst in removing heteroatoms from a hydrocarbon feedstock , the method comprising:hydrotreating a first hydrocarbon feedstock by contacting the first feedstock with a bulk catalyst containing at least three of the following metals: cobalt, nickel, molybdenum, and tungsten, said bulk catalyst in its unused state having a relative volumetric catalytic activity for hydrodesulfurization and/or hydrodenitrogenation, with the contacting being done under conditions effective to at least partially hydrodesulfurize and/or hydrodenitrogenate the first feedstock, wherein the contacting continues until the bulk catalyst exhibits a relative volumetric hydrodesulfurization activity of not more than 60% of the relative volumetric hydrodesulfurization activity in its unused state;isolating the hydrotreated first hydrocarbon feedstock;hydrotreating a second hydrocarbon feedstock by contacting the second feedstock with the bulk catalyst whose relative volumetric hydrodesulfurization activity is not more than 60% of the relative volumetric hydrodesulfurization activity in its unused state, with the contacting being done under conditions effective to at least partially hydrodesulfurize and/or hydrodenitrogenate the second feedstock, as well as to hydrodeoxygenate the second feedstock; andisolating the hydrotreated second hydrocarbon feedstock, wherein:the second hydrocarbon feedstock contains at least 10 wt % more biocomponent content than the first hydrocarbon feedstock;the first hydrocarbon feedstock has a pre-treated sulfur content, the hydrotreated first ...

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Номер записи: 50
27-02-2014 дата публикации

SELECTIVE HYDRODESULFURIZATION OF FCC GASOLINE TO BELOW 10 PPM SULFUR

Номер: US20140054198A1
Автор: Podrebarac Gary G.
Принадлежит: CATALYTIC DISTILLATION TECHNOLOGIES

A process for reducing the sulfur content of a hydrocarbon stream is disclosed. A full range cracked naphtha is contacted with a hydrogenation catalyst to convert at least a portion of the dienes and mercaptans to thioethers and to hydrogenate at least a portion of the dienes. The full range cracked naphtha is fractionated into a light naphtha fraction, a medium naphtha fraction, and a heavy naphtha fraction. The heavy naphtha fraction is hydrodesulfurized. The medium naphtha fraction is mixed with hydrogen and gas oil to form a mixture, which is contacted with a hydrodesulfurization catalyst to produce a medium naphtha fraction having a reduced sulfur concentration. The light, heavy, and medium naphtha fractions may then be recombined to form a hydrodesulfurized product having a sulfur content of less than 10 ppm in some embodiments. 1. A process for reducing the sulfur content of a hydrocarbon stream , the process comprising:contacting a full range cracked naphtha with a hydrogenation catalyst to convert at least a portion of the dienes and mercaptans to thioethers and to hydrogenate at least a portion of the dienes;fractionating the full range cracked naphtha into a light naphtha fraction, a medium naphtha fraction, and a heavy naphtha fraction;hydrodesulfurizing the heavy naphtha fraction;mixing the medium naphtha fraction with hydrogen and a gas oil to form a mixture;contacting the mixture with a hydrodesulfurization catalyst in a hydrodesulfurization reactor to produce a reactor effluent comprising hydrogen sulfide, unreacted hydrogen, and a medium naphtha fraction having a reduced sulfur concentration;separating the medium naphtha fraction having a reduced sulfur concentration from the gas oil, the unreacted hydrogen, and hydrogen sulfide.2. The process of claim 1 , wherein the light naphtha fraction has a boiling range end point in the range from about 120° F. to about 190° F.3. The process of claim 1 , wherein the medium naphtha fraction has a boiling range ...

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Номер записи: 51
27-03-2014 дата публикации

CONTROLLING TEMPERATURE WITHIN A CATALYST BED IN A REACTOR VESSEL

Номер: US20140083905A1
Автор: Daily Jeffrey N.
Принадлежит:

A quenching medium is delivered directly to selected regions or locations within a catalyst bed in a hydroprocessing reactor vessel in order to control the reactivity of a hydroprocess occurring in the selected regions or locations separately from other regions or locations. Temperature sensors for providing temperature indications and conduits for delivering the quench medium are distributed throughout the catalyst bed. One or more conduits can be selected for delivery of the quenching medium to selected regions or locations so that separate control of the level of reactivity in each of various regions or locations throughout the bed can be achieved. 1controlling reactivity of a hydroprocess occurring in a first region of catalyst material in a catalyst bed in response to a change of a characteristic of the catalyst material in the first region relative to the characteristic of the catalyst material in a second region; andcontrolling reactivity of the hydroprocess occurring in the second region of catalyst material in the catalyst bed in response to a change of the characteristic of the catalyst material in the second region relative to the characteristic of the catalyst material in the first region,wherein the reactivity of the hydroprocess occurring in the second region is controlled separately from controlling the reactivity of the hydroprocess occurring in the first region.. A method for use in a hydroprocessing reactor vessel containing a catalyst bed, comprising: This application is a continuation of U.S. application Ser. No. 13/154,111 filed on Jun. 6, 2011, the entirety of which is incorporated by reference herein.The present invention relates generally to controlling temperature, and, more particularly, to controlling temperature within a catalyst bed in a hydroprocessing reactor vessel.The petrochemical and refining industries generally process or treat a hydrocarbon material using various catalytic processes that are carried out in a reactor vessel. ...

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Номер записи: 52
01-01-2015 дата публикации

Generating cellulosic-renewable identification numbers in a refinery

Номер: US20150000186A1
Автор: Barry A. Freel, Robert G. Graham
Принадлежит: Ensyn Renewables Inc

The present application generally relates to methods of generating cellulosic-renewable identification numbers by thermally processing a cellulosic biomass to form a renewable fuel oil, and then co-processing the renewable fuel oil with a petroleum fraction in a refinery to form a cellulosic-renewable identification number-compliant fuel.

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Номер записи: 53
01-01-2015 дата публикации

PROCESS AND APPARATUS FOR PRODUCING DIESEL

Номер: US20150001129A1
Автор: Kokayeff Peter, Sadler Clayton C., Thakkar Vasant P.
Принадлежит:

A process and apparatus is disclosed for pretreating a hydrocarbon stream in a hydrotreating reactor and separating the diesel materials from the pretreated effluent before the heavier liquid materials are fed to a hydrocracking unit. Thus diesel materials are preserved but recovered along with the hydrocracked effluent. A recovered diesel stream can be sent to a hydrotreating unit to improve its cetane rating. 1. A process for producing diesel from a hydrocarbon stream comprising:feeding a hydrocarbon stream to a hydrotreating reactor;hydrotreating the hydrocarbon stream in the presence of a hydrogen stream and pretreating catalyst to provide a pretreated effluent stream;separating said pretreated effluent stream into a vaporous pretreated stream and a liquid pretreated stream;hydrocracking the liquid pretreated stream in the presence of hydrocracking catalyst and hydrogen to provide a hydrocracking effluent stream;mixing said vaporous pretreated stream with said hydrocracking effluent stream to provide a mixed hydrocracking effluent stream;fractionating at least a portion of the mixed hydrocracking effluent stream to provide a diesel stream; andhydrotreating the diesel stream in the presence of a hydrotreating hydrogen stream and hydrotreating catalyst to provide a hydrotreating effluent stream.2. The process of further comprising separating at least a portion of the mixed hydrocracking effluent stream into a vaporous mixed hydrocracking effluent stream comprising hydrogen and a liquid mixed hydrocracking effluent stream.3. The process of wherein the hydrotreating reactor comprises a catalyst selected from a noble metal catalyst claim 1 , a desulfurization catalyst claim 1 , an isomerization catalyst and an aromatic saturation catalyst.4. The process of wherein the entire vaporous pretreated stream is mixed with the hydrocracking effluent stream.5. The process of wherein the vaporous pretreated stream is mixed with the entire hydrocracking effluent stream.6. The ...

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Номер записи: 54
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: 55
03-01-2019 дата публикации

METHOD FOR KETONISATION OF BIOLOGICAL MATERIAL

Номер: US20190002382A1
Автор: KETTUNEN Mika, MYLLYOJA Jukka, Piilola Rami
Принадлежит: Neste Oyj

A method for producing ketones includes a) providing a feedstock of biological origin having fatty acids and/or fatty acid derivatives having an average chain length of 24 C-atoms or less; b) subjecting the feedstock to a catalytic ketonisation reaction in the presence of aK2O/TiO2-catalyst; and c) obtaining from the ketonisation reaction a product stream having ketones, which ketones have a longer average hydrocarbon chain length than the average hydrocarbon chain length in the feedstock, wherein step b) is carried out directly on the feedstock and in the presence of the K2O/TiO2-catalyst as the sole catalyst applied in the ketonisation reaction. 1. A method for producing ketones , which method comprises:a) providing a feedstock of biological origin containing fatty acids and/or fatty acid derivatives having an average chain length of 24 C-atoms or less;{'sub': 2', '2, 'b) subjecting said feedstock to a catalytic ketonisation reaction in a presence of a KO/TiO-catalyst; and'}c) obtaining from said ketonisation reaction a product stream containing ketones, which ketones have a longer average hydrocarbon chain length than the average hydrocarbon chain length in said feedstock;{'sub': 2', '2, 'wherein the subjecting is carried out directly on said feedstock and in a presence of said KO/TiO-catalyst as a sole catalyst applied in said ketonisation reaction.'}2. The method according to claim 1 , wherein the subjecting is carried out directly on said feedstock without preceding or simultaneous hydrogenation of double bonds present in the fatty acids and/or fatty acid derivatives in said feedstock.3. The method according to claim 1 , comprising:performing said ketonisation reaction by introducing the feedstock in liquid phase.4. The method according to claim 1 , wherein said feedstock of biological origin contains unsaturated fatty acids and/or fatty acid derivatives claim 1 , or esters.5. The method according to claim 1 , comprising:performing said ketonisation reaction ...

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Номер записи: 56
04-01-2018 дата публикации

PRODUCTION OF LOW CLOUD POINT DISTILLATE FUELS

Номер: US20180002615A1
Автор: CHUBA Michael R., Hilbert Timothy L., Kalyanaraman Mohan, Patel Bryan A., Shih Stuart S., Skoulidas Anastasios I., SMYTH Sean C.
Принадлежит:

Systems and methods are provided for catalytically dewaxing a diesel boiling range feed. In some aspects, catalytic dewaxing can be performed at low hydrogen treat gas rates and/or low hydrogen purity conditions. In other aspects, the systems and methods can allow for distillate dewaxing while reducing or minimizing the amount of equipment required. 1. A method for producing distillate fuel boiling range material , comprising:{'sup': 3', '3', '3', '3, 'sub': '2', 'exposing a distillate fuel boiling range feedstock having a sulfur content of about 15 wppm or less to a dewaxing catalyst comprising a molecular sieve and a metal hydrogenation component under dewaxing conditions to produce a dewaxed effluent comprising a distillate fuel boiling range product and/or blendstock having a cloud point that is reduced relative to a cloud point of the feedstock by at least about 5° C., the dewaxing conditions comprising a total pressure of about 200 psig (about 1.4 MPag) or less, a hydrogen partial pressure of about 100 psig (about 700 kPag) or less, and a treat gas rate of about 100 SCF/bbl (about 17 Nm/m) to about 5000 SCF/bbl (about 850 Nm/m) of a treat gas comprising about 5 vol % to about 50 vol % H.'}2. The method of claim 1 , wherein the vol % of Hin the treat gas is lower than a vol % of Hin a gaseous portion of the dewaxed effluent.3. The method of claim 1 , wherein the treat gas has a sulfur content of about 0.001 vol % or less.4. The method of claim 1 , wherein the dewaxing conditions further comprise a temperature of from about 500° F. (˜260° C.) to about 750° F. (˜399° C.) and a space velocity from about 0.3 hrto about 5.0 hr.5. The method of claim 1 , further comprising exposing a second feedstock to a hydrotreating catalyst to form a hydrotreated effluent claim 1 , and separating the hydrotreated effluent to form the distillate fuel boiling range feedstock.6. The method of claim 5 , wherein the effective hydrotreating conditions comprise a pressure from about 200 ...

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Номер записи: 57
04-01-2018 дата публикации

PROCESS AND APPARATUS FOR HYDROCRACKING AND HYDROISOMERIZING A HYDROCARBON STREAM

Номер: US20180002616A1
Автор: Kumar Sailesh B., Petri John A., Sangalli Massimo, Thakkar Vasant P., Towarnicky Andrew J.
Принадлежит:

A process and apparatus for quenching a hydrocracked stream to prepare it for hydroisomerization. A fractionated hydroisomerized stream is recycled to quench a hot hydrocracked stream prior to hydroisomerization. Sufficient quenching can inactivate the hydroisomerization catalyst bed. The hydroisomerization catalyst bed can be heated back to hydroisomerization temperature and can actively hydroisomerize again. 1. A process for hydrocracking and hydroisomerizing a hydrocarbon stream comprising:hydrocracking a hydrocarbon feed stream over a first hydrocracking catalyst bed to provide a hydrocracked stream;hydroisomerizing said hydrocracked stream over a first hydroisomerization catalyst bed to provide a hydroisomerized stream;fractionating said hydroisomerized stream in a fractionation section to provide a first fractionated stream; andrecycling a first fractionated stream to said first isomerization catalyst bed to quench said hydrocracked stream.2. The process of further comprising hydrocracking a second fractionated stream over said first hydrocracking catalyst bed.3. The process of further comprising hydrocracking a second fractionated stream over a second hydrocracking catalyst bed to provide a second hydrocracked stream.4. The process of wherein said first hydrocracking catalyst bed and said first hydroisomerization catalyst bed are located in a first reactor and said second hydrocracking catalyst bed is located in a second reactor.5. The process of further comprising cooling said first fractionated stream to inactivate said first hydroisomerization catalyst bed.6. The process of wherein said fractionation comprises stripping gases from said hydroisomerized stream to provide a stripped stream and recycling a portion of said stripped stream to said first isomerization catalyst bed as said first fractionated stream.7. The process of wherein said fractionation comprises fractionating said hydroisomerized stream under vacuum and recycling a vacuum fractionated ...

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Номер записи: 58
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: 59
03-01-2019 дата публикации

Multi-Stage Process and Device for Distributive Production of a Low Sulfur Heavy Marine Fuel Oil

Номер: US20190002772A1
Автор: Klussmann Bertrand Ray, Moore Michael Joseph, White Carter James
Принадлежит: Magēmā Technology, LLC

A multi-stage process for the distributive production of an ISO8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process that is distributed in a Reaction System composed of multiple reaction vessels. 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 distributive process is disclosed that can utilize a modular reactor vessel contained within a frame work based on ISO 40 foot or ISO 20 foot container dimensions. 1. A process for the distributive production of a 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 in a Reaction System to form a Process Mixture from said Feedstock Mixture; receiving said Process Mixture and separating the liquid components of the Process Mixture from the bulk gaseous components of the Process Mixture; subsequently separating any residual gaseous components and by-product hydrocarbon components from the Product Heavy Marine Fuel Oil; and , discharging the Product Heavy Marine Fuel Oil; wherein the Reaction System comprises two or more reactor vessels wherein said reactor vessels are configured in a matrix of at least 2 reactors by 2 reactors.2. The process of wherein the Feedstock Heavy Marine Fuel Oil complies with ISO 8217 (2017) and has a sulfur content (ISO 14596 or ISO 8754) between the range of 5.0 mass % to 1.0 mass % and wherein the Product Heavy Marine Fuel Oil complies with ISO 8217 (2017) and has a sulfur content (ISO 14596 or ISO 8754) between the range of 0.50 mass % to 0.05 mass %.3. The process of claim 2 , wherein said Feedstock Heavy Marine Fuel Oil has: a maximum of kinematic ...

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Номер записи: 60
01-01-2015 дата публикации

Fluidized catalytic cracking apparatus

Номер: US20150004067A1
Автор: Barry A. Freel, Robert G. Graham
Принадлежит: Ensyn Renewables Inc

The present application generally relates to a fluidized catalytic cracking apparatus having one or more ports for injecting a renewable fuel oil for co-processing the renewable fuel oil and a petroleum fraction.

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Номер записи: 61
01-01-2015 дата публикации

Process and apparatus for producing diesel

Номер: US20150004072A1
Автор: Clayton C. Sadler, Peter Kokayeff, Vasant P. Thakkar
Принадлежит: UOP LLC

A process and apparatus is disclosed for pretreating a hydrocarbon stream in a hydrotreating reactor and separating the diesel materials from the pretreated effluent before the heavier liquid materials are fed to a hydrocracking unit. Thus diesel materials are preserved but recovered along with the hydrocracked effluent. A recovered diesel stream can be sent to a hydrotreating unit to improve its cetane rating.

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Номер записи: 62
12-01-2017 дата публикации

CONVERSION OF BIOMASS OR RESIDUAL WASTE MATERIAL TO BIOFUELS

Номер: US20170009143A1
Автор: CHILKOOR SOUNDARARAJAN Laxmi Narasimhan, DEL PAGGIO Alan Anthony, Gopal Srikant, PANCHAGNULA Madhusudhan Rao, URADE Vikrant Nanasaheb
Принадлежит:

The present invention provides a process for producing liquid hydrocarbon products from solid biomass and/or residual waste feedstocks, said process comprising the steps of: a) hydropyrolysing the solid feedstock in a hydropyrolysis reactor vessel in the presence of molecular hydrogen and one or more deoxygenation catalyst, producing a product stream comprising partially deoxygenated hydropyrolysis product, HO, H, CO, CO, C-Cgases, char and catalyst fines; b) removing said char and catalyst fines from said product stream; c) hydroconverting said partially deoxygenated hydropyrolysis product in a hydroconversion reactor vessel in the presence of one or more hydroconversion catalyst and of the HO, CO, CO, H, and C-Cgas generated in step a), producing a vapour phase product comprising substantially fully deoxygenated hydrocarbon product, HO, CO, CO, and C-Cgases; d) condensing the vapour phase product of step d) to provide a liquid phase product comprising substantially fully deoxygenated C4+ hydrocarbon liquid and aqueous material and separating said liquid phase product from a gas phase product comprising H, CO, CO, and C-Cgases; e) removing the aqueous material from the substantially fully deoxygenated C4+ hydrocarbon liquid; and f) hydroprocessing at least a portion of the substantially fully deoxygenated C4+ hydrocarbon liquid in a hydroprocessing reactor vessel in the presence of hydrogen and one or more hydroprocessing catalysts, each hydroprocessing catalyst comprising at least one reduced metal on a solid support, in order to provide an upgraded liquid hydrocarbon stream. 1. A process for producing liquid hydrocarbon products from solid biomass and/or residual waste feedstocks , said process comprising the steps of:{'sub': 2', '2', '2', '1', '3, 'a) hydropyrolysing the solid feedstock in a hydropyrolysis reactor vessel in the presence of molecular hydrogen and one or more deoxygenation catalyst, producing a product stream comprising partially deoxygenated ...

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Номер записи: 63
12-01-2017 дата публикации

COMPOSITION COMPRISING PARAFFIN FRACTIONS OBTAINED FROM BIOLOGICAL RAW MATERIALS AND METHOD OF PRODUCING SAME

Номер: US20170009144A1
Автор: Aalto Pekka, HAKOLA Maija, NYMAN Tomi, Sandberg Kati
Принадлежит: Neste Oyj

A composition, including 40-50 wt-% C14 paraffins, based on the total weight of the composition, and 35-45 wt-% C15 paraffins, based on the total weight of the composition, wherein the C14 and C15 paraffins are produced from a biological raw material. 119-. (canceled)20. A composition , comprising:40-50 wt-% C14 isoparaffins, based on the total weight of the composition, and35-45 wt-% C15 isoparaffins, based on the total weight of the composition,wherein the C14 and C15 isoparaffins are produced from a biological raw material,wherein the total C14 and C15 isoparaffinic content of the composition is in a range from 80.36 wt-% to 95 wt-%, based on the total weight of the composition.21. The composition according to claim 20 , wherein the composition comprises 45-50 wt-% C14 isoparaffins claim 20 , and 40-45 wt-% C15 isoparaffins claim 20 , based on the total weight of the composition.22. The composition according to claim 20 , wherein the composition comprises less than 9 wt-% C13 and lighter paraffins and less than 7 wt-% C16 and heavier paraffins claim 20 , based on the total weight of the composition.23. The composition according to claim 20 , wherein the composition comprises less than 5 wt-% C13 and lighter paraffins and less than 3 wt-% C16 and heavier paraffins claim 20 , based on the total weight of the composition.24. The composition according to claim 20 , wherein the total isoparaffinic content of the composition is more than 93 wt-% claim 20 , based on the total weight of the composition.25. The composition according to claim 20 , wherein the total isoparaffinic content of the composition is more than 97 wt-% claim 20 , based on the total weight of the composition.26. The composition according to claim 20 , wherein the total aromatic hydrocarbon content of the composition is less than 1500 ppm weight basis.27. The composition according to claim 20 , wherein the total aromatic hydrocarbon content of the composition is less than 1300 ppm weight basis.28. The ...

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Номер записи: 64
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: 65
08-01-2015 дата публикации

High Density Cyclic Fuels Derived From Linear Sesquiterpenes

Номер: US20150011810A1
Автор: Benjamin G Harvey
Принадлежит: US Department of Navy

A method to generate cyclic hydrocarbons from farnesene to increase both the density and net heat of combustion of the product fuels. The high density hydrocarbons produced by this method have applications for missile, UAV, jet, and diesel propulsion.

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Номер записи: 66
10-01-2019 дата публикации

HYDROPROCESSING OF HIGH DENSITY CRACKED FRACTIONS

Номер: US20190010410A1
Автор: Brown Stephen H., CUNNINGHAM Brian A., ILIAS Samia, McMANUS Jesse R., Smiley Randolph J.
Принадлежит:

Systems and methods are provided for upgrading a high density cracked feedstock, such as a catalytic slurry oil, by hydroprocessing. The upgrading can further include performing a separation on the effluent from hydroprocessing of the cracked feedstock, such as a distillation (i.e., separation based on boiling point) or a solvent-based separation. The separation on the hydroprocessed effluent can allow for separation of an aromatics-enriched fraction and an aromatics-depleted fraction from the hydroprocessed effluent. The aromatics-enriched fraction and aromatics-depleted fraction can then be separately used and/or separately undergo further processing. 1. A method for processing a heavy cracked feedstock , comprising:{'sup': 3', '3, 'exposing a feedstock comprising a density at 15° C. of 1.06 g/cmor more and at least 50 wt % of one or more 343° C.+ cracked fractions to a hydroprocessing catalyst under fixed bed hydroprocessing conditions to form a hydroprocessed effluent, the one or more 343° C.+ cracked fractions having an aromatics content of 40 wt % or more relative to a weight of the one or more 343° C.+ cracked fractions, a 343° C.+ portion of the hydroprocessed effluent having a density at 15° C. of 1.04 g/cmor less;'}separating the hydroprocessed effluent in one or more separation stages to form an aromatics-enriched fraction and an aromatics-depleted fraction; andexposing at least a portion of the aromatics-enriched fraction to a second hydroprocessing catalyst under second fixed bed hydroprocessing conditions to form a second hydroprocessed effluent.2. The method of claim 1 , wherein exposing the feedstock to the hydroprocessing catalyst further comprises exposing the at least a portion of the aromatics-enriched fraction to the hydroprocessing catalyst claim 1 , wherein the hydroprocessing conditions comprise the second hydroprocessing conditions claim 1 , and wherein the hydroprocessed effluent comprises the second hydroprocessed effluent.3. The method of ...

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Номер записи: 67
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: 68
15-01-2015 дата публикации

SLURRY HYDROCONVERSION WITH HIGH ACTIVITY CATALYSTS

Номер: US20150014216A1
Автор: Billimoria Rustom Merwan, Degnan, JR. Thomas Francis, Smiley Randolph J., Sundararaman Ramanathan, Thiart Jacob Johannes, Wilson Keith
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Systems and methods are provided for slurry hydroconversion of a heavy oil feed, such as an atmospheric or vacuum resid. The systems and methods allow for slurry hydroconversion using catalysts with enhanced activity. The catalysts with enhanced activity can be used in conjunction with demetallization catalysts or catalysts that can be recycled as a side product from a complementary refinery process. 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.) and a first Conradson carbon residue wt %;exposing the heavy oil feedstock to a slurry hydroconversion catalyst in one or more reactors under effective slurry hydroconversion conditions to form a slurry hydroconversion effluent, the effective slurry hydroconversion conditions being effective for conversion of at least about 80 wt % of the second heavy oil feedstock relative to a conversion temperature of 1050° F. (566° C.), such as at least about 90 wt %;separating a bottoms product from the slurry hydroconversion effluent, the bottoms product having a 10% distillation point of at least about 650° F. (343° C.); and 'wherein the slurry hydroconversion catalyst comprises a bulk multimetallic catalyst comprising at least one non-noble Group VIII (Group 8-10) metal and at least one Group VIB (Group 6) metal, a weight of the slurry hydroconversion catalyst being about 2 wt % to 25 wt % of a weight of the heavy oil feedstock in the reactor.', 'hydrocracking at least a portion of the bottoms product in the presence of a hydrocracking catalyst under effective hydrocracking conditions, the at least a portion of the bottoms product having a final boiling point of at least about 1050° F. (566° C.),'}2. The method of claim 1 , wherein the bottoms product has a nitrogen content of about 500 wppm or less.3. The method of claim 1 , wherein the bottoms product is separated from the slurry hydroconversion effluent without ...

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Номер записи: 69
15-01-2015 дата публикации

INTEGRATED HYDROCRACKING AND SLURRY HYDROCONVERSION OF HEAVY OILS

Номер: US20150014217A1
Автор: Billimoria Rustom Merwan, Dandekar Ajit Bhaskar, Degnan, JR. Thomas Francis, Smiley Randolph J., Sundararaman Ramanathan
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Improved yields of fuels and/or lubricants from a resid or other heavy oil feed can be achieved using slurry hydroconversion to convert at least about 90 wt % of the feed. The converted portion of the feed can then be passed into one or more hydroprocessing stages. An initial processing stage can be a hydrotreatment stage for additional removal of contaminants and for passivation of high activity functional groups that may be created during slurry hydroconversion. The hydrotreatment effluent can then be fractionated to separate naphtha boiling range fractions from distillate fuel boiling range fractions and lubricant boiling range fractions. At least the lubricant boiling range fraction can then be hydrocracked to improve the viscosity properties. The hydrocracking effluent can also be dewaxed to improve the cold flow properties. The hydrocracked and/or dewaxed product can then be optionally hydrofinished. 1. A method for processing a heavy oil feedstock , comprising:providing a heavy oil feedstock having a 5 wt % boiling point of at least about 650° F. (343° C.) and a first Conradson carbon residue wt %;exposing the heavy oil feedstock to a catalyst under effective slurry hydroconversion conditions to form at least a first liquid product, the effective slurry hydroconversion conditions being effective for conversion of at least about 90 wt % of the heavy oil feedstock relative to a conversion temperature;hydrotreating the first liquid product under effective hydrotreating conditions to form a first hydrotreated liquid product;fractionating the first hydrotreated liquid product to form one or more naphtha boiling range products, one or more distillate fuel boiling range products, and one or more lubricating base oil boiling range products; andhydrocracking at least a portion of the one or more lubricating base oil boiling range products to form at least one hydrocracked fuel product and a hydrocracking bottoms product.2. The method of claim 1 , further comprising ...

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Номер записи: 70
15-01-2015 дата публикации

Hydrotreating Process and Apparatus

Номер: US20150014218A1
Автор: Banerjee Soumendra, Bisht Deepak
Принадлежит:

A process for hydrotreating full range naphtha is disclosed including the steps of passing a vapor stream composed of naphtha hydrocarbons to a first catalyst bed of a hydrotreating reactor, passing a liquid stream composed of naphtha hydrocarbons to a second catalyst bed of the hydrotreating reactor, and recovering a hydrotreated product stream from the hydrotreating reactor. The first and second catalyst beds are arranged in series within the hydrotreating reactor, and the second catalyst bed is downstream of the first catalyst bed. 1. A process for hydrotreating full range naphtha , the process comprising:(a) passing a vapor stream comprising naphtha hydrocarbons to a first catalyst bed of a hydrotreating reactor;(b) passing a liquid stream comprising naphtha hydrocarbons to a second catalyst bed of the hydrotreating reactor; and(c) recovering a hydrotreated product stream from the hydrotreating reactor;wherein the first and second catalyst beds are arranged in series within the hydrotreating reactor, and the second catalyst bed is downstream of the first catalyst bed.2. The process of claim 1 , wherein:the liquid stream further comprises a heavy naphtha fraction and a medium naphtha fraction and the vapor stream further comprises a heavy naphtha fraction.3. The process of claim 2 , further comprising:separating a full range naphtha feedstock into a plurality of fractions comprising the medium naphtha fraction and the heavy naphtha fraction;passing the heavy naphtha fraction to a vapor-liquid separation unit to produce the vapor stream and a heavy naphtha liquid stream; andadmixing the medium naphtha fraction with the heavy naphtha liquid stream to produce the liquid stream.4. The process of claim 3 , wherein separating the full range naphtha feedstock involves distillation.5. The process of claim 3 , wherein the plurality of fractions further comprises a light naphtha fraction.6. The process of claim 5 , wherein the light naphtha fraction comprises naphtha ...

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Номер записи: 71
03-02-2022 дата публикации

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Номер: US20220033724A1
Автор: Pruitt Tom F., Wohaibi Mohammed
Принадлежит: MAWETAL LLC

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 138-. (canceled)393241. Combustion in marine or land based engines , combustion gas turbines , or fired heaters of a fuel derived from light tight oil () and crude oil () , either alone or with added high sulfur fuel oil () , comprising combination of treated and untreated streams having an initial boiling point being the lowest boiling point of any fraction within untreated streams combined in said fuel and highest boiling point being the highest boiling portion of deasphalted oil effluent from solvent separation of an unconverted oil which is subsequently treated by hydroconversion and forms a portion said fuel.4055-. (canceled)56. Combustion of a fuel in accordance with wherein said fuel comprises a portion or all of a light tight oil and streams of processed high sulfur fuel oil claim 39 , processed alone or with added crude oil claim 39 , comprising:(a) unstabilized wild straight run naphtha and distillation fraction at or below sulfur breakpoint cut without added treatment,(b) distillate hydrotreater effluent of distillate range distillation fraction above sulfur breakpoint cut comprising wild naphtha and at least a portion of ...

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Номер записи: 72
19-01-2017 дата публикации

Production of low sulfur gasoline

Номер: US20170015915A1
Автор: Bryan C. Lu, John P. Greeley, Michael R. Chuba, Mohsen N. Harandi
Принадлежит: ExxonMobil Research and Engineering Co

Systems and methods are provided for producing naphtha boiling range fractions having a reduced or minimized amount of sulfur and an increased and/or desirable octane rating and suitable for incorporation into a naphtha fuel product. A naphtha boiling range feed can be separated to form a lower boiling portion and a higher boiling portion. The lower boiling portion, containing a substantial amount of olefins, can be exposed to an acidic catalyst without the need for providing added hydrogen in the reaction environment. Additionally, during the exposure of the lower boiling portion to the acidic catalyst, a stream of light olefins (such as C 2 -C 4 olefins) can be introduced into the reaction environment. Adding such light olefins can enhance the C 5 + yield and/or improve the removal of sulfur from thiophene and methyl-thiophene compounds in the naphtha feed.

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Номер записи: 73
17-01-2019 дата публикации

METHOD TO REMOVE SULFUR AND METALS FROM PETROLEUM

Номер: US20190016967A1
Автор: ALQARZOUH Muneef F., Choi Ki-Hyouk, Punetha Ashok K.
Принадлежит: Saudi Arabian Oil Company

A method to selectively remove metal compounds and sulfur from a petroleum feedstock is provided. The method comprising the steps of feeding a pre-heated water stream and a pre-heated petroleum feedstock to a mixing zone, mixing the pre-heated water stream and the pre-heated petroleum feedstock to form a mixed stream, introducing the mixed stream to a first supercritical water reactor to produce an upgraded stream, combining the upgraded stream and a make-up water stream in a make-up mixing zone to produce a diluted stream, wherein the make-up water stream increases the ratio of water to oil in the diluted stream as compared to the upgraded stream, and introducing the diluted stream to a second supercritical water reactor to produce a product effluent stream. The method can include mixing a carbon with the make-up water stream. 1. A system to selectively remove metal compounds and sulfur from a petroleum feedstock , the system comprising:a mixing zone, the mixing zone configured to mix a pre-heated water stream and a pre-heated petroleum feedstock to form a mixed stream, wherein the pre-heated water stream is at a temperature above the critical temperature of water and at a pressure above the critical pressure of water, wherein the pre-heated petroleum feedstock is at a temperature of less than 150° C. and at a pressure above the critical pressure of water, wherein the pre-heated petroleum feedstock comprises a petroleum feedstock;a first supercritical water reactor fluidly connected to the mixing zone, the first supercritical water reactor configured to allow conversion reactions to occur to produce an upgraded stream, the first supercritical water reactor at a pressure above the critical pressure of water and at a temperature above the critical temperature of water, the first supercritical water reactor in the absence of externally provided hydrogen;a carbon dispersal zone, the carbon dispersal zone configured to mix carbon with a make-up water stream to produce a ...

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Номер записи: 74
17-01-2019 дата публикации

Multistage Upgrading Hydrocarbon Pyrolysis Tar

Номер: US20190016969A1
Автор: Coleman John S., Kandel Kapil, Koc-Karabocek Reyyan, Nayak Subramanya V., Patel Bryan A., Rachal Cyrus J., Raman Sumathy, Xu Teng
Принадлежит:

A multi-stage process for upgrading tars is provided. A predominantly hydrotreating stage can be applied before a cracking stage, which can be a hydrocracking or a thermal cracking stage. Alternatively, a predominantly cracking stage, which can be a hydrocracking or a thermal cracking stage, can be applied before a hydrotreating stage. Apparatus suitable for performing the method is also provided. 1. A hydrocarbon conversion process , comprising: [{'sub': 'N', '≥10.0 wt. % pyrolysis tar hydrocarbon based on the weight of the feedstock, the pyrolysis tar having a I≥100 and viscosity measured at 50° C. of ≥10,000 cSt, and'}, 'a utility fluid comprising aromatic hydrocarbons and having an ASTM D86 10% distillation point >60° C. and a 90% distillation point <425° C.; and, '(a) providing a feedstock comprising(b) hydroprocessing the feedstock in at least two hydroprocessing zones in the presence of a treat gas comprising molecular hydrogen under catalytic hydroprocessing conditions to produce a hydroprocessed product, comprising hydroprocessed tar;wherein the hydroprocessing conditions are such that in a first hydroprocessing zone a catalyst is used that promotes predominantly a hydrotreating reaction and in a second hydroprocessing zone a catalyst is used that promotes predominantly a hydrocracking reaction.2. The process of claim 1 , in which the catalyst in the first hydroprocessing zone comprises one or more of Mo claim 1 , Co and Ni claim 1 , supported on alumina claim 1 , Pt—Pd/AlO—SiO claim 1 , Ni—W/AlO claim 1 , Ni—Mo/AlO claim 1 , Fe claim 1 , or Fe—Mo supported on a non-acidic support such as carbon black or a carbon black composite claim 1 , or Mo supported on a nonacidic support claim 1 , and the catalyst in the second hydroprocessing zone comprises predominantly a zeolite or comprises predominantly Co claim 1 , Mo claim 1 , P claim 1 , Ni or Pd supported on amorphous AlOand/or SiO(ASA) and/or zeolite.3. The process of claim 1 , in which the catalyst in the ...

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Номер записи: 75
17-01-2019 дата публикации

SYSTEMS AND METHODS FOR PROCESSING HEAVY OILS BY OIL UPGRADING FOLLOWED BY STEAM CRACKING

Номер: US20190016970A1
Автор: Abba Ibrahim, BOURANE Abdennour, Ding Lianhui, Shaik Kareemuddin, Tamimi Mazin
Принадлежит: Saudi Arabian Oil Company

According to one embodiment, a heavy oil may be processed by a method that may include upgrading at least a portion of the heavy oil to form an upgraded oil, where the upgrading includes contacting the heavy oil with a hydrodemetalization catalyst, a transition catalyst, a hydrodenitrogenation catalyst, and a hydrocracking catalyst to remove at least a portion of metals, nitrogen, or aromatics content from the heavy oil and form the upgraded oil; and passing the upgraded oil to a steam cracker and steam cracking the upgraded oil to form a steam-cracked effluent; and where the final boiling point of the upgraded oil is less than or equal to 540° C. 1. A method for processing heavy oil , the method comprising:upgrading at least a portion of the heavy oil to form an upgraded oil, the upgrading comprising contacting the heavy oil with a hydrodemetalization catalyst, a transition catalyst, a hydrodenitrogenation catalyst, and a hydrocracking catalyst to remove at least a portion of metals, nitrogen, or aromatics content from the heavy oil and form the upgraded oil; andpassing the upgraded oil to a steam cracker and steam cracking the upgraded oil to form a steam-cracked effluent;wherein the final boiling point of the upgraded oil is less than or equal to 540° C.2. The method of claim 1 , wherein the feed oil is crude oil having an American Petroleum Institute (API) gravity of from 25 degrees to 50 degrees.3. The method of claim 1 , further comprising:separating a feed oil into a heavy feed fraction and a light feed fraction; andpassing the light feed fraction to the steam cracker;wherein the heavy feed fraction is the heavy oil that is upgraded.4. The method of claim 3 , wherein the cut point of the light feed fraction relative to the heavy feed fraction is from 300° C. to 400° C.5. The method of claim 3 , wherein the cut point of the light feed fraction and heavy feed fraction is from 120° C. to 230° C.6. The method of claim 1 , wherein:the hydrodemetalization catalyst, ...

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Номер записи: 76
17-01-2019 дата публикации

Systems and methods for processing heavy oils by oil upgrading followed by distillation

Номер: US20190016971A1
Автор: Abdennour Bourane, Ibrahim Abba, Kareemuddin SHAIK, Lianhui Ding, Mazin Tamimi
Принадлежит: Saudi Arabian Oil Co

According to one embodiment, a heavy oil may be processed by a method that may include upgrading at least a portion of the heavy oil to form an upgraded oil, where the upgrading comprises contacting the heavy oil with a hydrodemetalization catalyst, a transition catalyst, a hydrodenitrogenation catalyst, and a hydrocracking catalyst to remove at least a portion of metals, nitrogen, or aromatics content from the heavy oil and form the upgraded oil. The method may further include passing at least a portion of the upgraded oil to a separation device that separates the upgraded oil into one or more transportation fuels; and where the final boiling point of the upgraded oil is less than or equal to 540° C.

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Номер записи: 77
17-01-2019 дата публикации

SYSTEMS AND METHODS FOR PROCESSING HEAVY OILS BY OIL UPGRADING FOLLOWED BY REFINING

Номер: US20190016976A1
Автор: Abba Ibrahim, BOURANE Abdennour, Ding Lianhui, Shaik Kareemuddin, Tamimi Mazin
Принадлежит: Saudi Arabian Oil Company

According to one embodiment, a heavy oil may be processed by a method that may include upgrading at least a portion of the heavy oil to form an upgraded oil, where the upgrading includes contacting the heavy oil with a hydrodemetalization catalyst, a transition catalyst, a hydrodenitrogenation catalyst, and a hydrocracking catalyst to remove at least a portion of metals, nitrogen, or aromatics content from the heavy oil and form the upgraded oil. The method may further include passing at least a portion of the upgraded oil to a refinery operation. 1. A method for processing heavy oil , the method comprising:upgrading at least a portion of the heavy oil to form an upgraded oil, the upgrading comprising contacting the heavy oil with a hydrodemetalization catalyst, a transition catalyst, a hydrodenitrogenation catalyst, and a hydrocracking catalyst to remove at least a portion of metals, nitrogen, or aromatics content from the heavy oil and form the upgraded oil; andpassing at least a portion of the upgraded oil to a refinery operation.2. The method of claim 1 , wherein:the final boiling point of the upgraded oil is less than or equal to 540° C.;at least the heaviest components of the upgraded oil are passed to the refinery operation;or both.3. The method of claim 1 , wherein the hydrodemetalization catalyst claim 1 , the transition catalyst claim 1 , and the hydrodenitrogenation catalyst are positioned in series in a plurality of reactors; andwherein the hydrocracking catalyst is positioned in a reactor downstream of the plurality of reactors.4. The method of claim 3 , wherein the reactor downstream of the plurality of reactors is a packed bed reactor.5. The method of claim 3 , wherein the reactor downstream of the plurality of reactors is a fluidized bed reactor.6. The method of claim 1 , wherein the refinery operation is a coking refinery.7. The method of claim 6 , wherein the coking refinery comprises a hydrocracking process unit.8. The method of claim 6 , wherein ...

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Номер записи: 78
17-01-2019 дата публикации

PROCESS FOR PRODUCING NAPHTHENIC BASE OILS

Номер: US20190016978A1
Автор: Casserly Edward William, Davis Howard Don, Patrick John K.
Принадлежит:

A process for producing naphthenic base oils from low quality naphthenic crude feedstocks. The naphthenic base oils produced by the process have improved low temperature properties at high yields based on feedstock. 153.-. (canceled)54. A process for producing a naphthenic base oil comprising the steps of:a) hydrotreating a naphthenic feedstock having a sulfur content of up to about 5% by weight (as measured by ASTM D4294) and a nitrogen content of up to about 3% by weight (as measured by ASTM D5762) in the presence of a hydrotreating catalyst and hydrotreating conditions to produce a hydrotreated naphthenic effluent;b) dewaxing the hydrotreated naphthenic effluent having a sulfur content of about 0.0005% to about 0.5% by weight (as measured by ASTM D4294) and a nitrogen content of up to about 0.1% by weight (as measured by ASTM D5762) in the presence of a dewaxing cracking catalyst and under catalytic dewaxing conditions to produce a dewaxed effluent;c) hydrofinishing the dewaxed effluent in the presence of a hydrofinishing catalyst and under catalytic hydrofinishing conditions to produce a dewaxed hydrofinished effluent having reduced levels of polycyclic aromatic hydrocarbon compounds and reduced levels of unstable olefinic compounds; andd) fractionating the dewaxed hydrofinished effluent to remove one or more low viscosity high volatility fractions and provide a naphthenic base oil having a pour point (as measured by ASTM D5949) below about −5° C., at a yield greater than 85% of total naphthenic base oil over total hydrotreated naphthenic feedstock.55. The process of claim 54 , wherein the naphthenic feedstock comprises naphthenic crude claim 54 , waxy naphthenic crude claim 54 , naphthenic distillate or a mixture thereof.56. The process of claim 54 , wherein the naphthenic feedstock comprises a blend of naphthenic crude claim 54 , waxy naphthenic crude or a naphthenic distillate with paraffinic feedstock claim 54 , paraffinic distillate claim 54 , light or ...

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Номер записи: 79
17-01-2019 дата публикации

MULTI-STAGE UPGRADING PYROLYSIS TAR PRODUCTS

Номер: US20190016980A1
Автор: FERRUGHELLI David T., Kar Kenneth Chi Hang, MENNITO Anthony S., Rubin-Pitel Sheryl B., Xu Teng
Принадлежит:

A first hydroprocessed product and a second hydroprocessed product produced from a multi-stage process for upgrading pyrolysis tar, such as steam cracker tar, are provided herein. Fuel blends including the first hydroprocessed product and/or the second hydroprocessed product are also provided herein as well as methods of lowering pour point of a gas oil using the first hydroprocessed product and the second hydroprocessed product. 1. A first hydroprocessed product comprising:aromatics in an amount ≥about 50 wt %;paraffins in an amount ≤about 5.0 wt %; andsulfur in an amount from about 0.10 wt % to <0.50 wt %; a boiling point distribution of about 145° C. to about 760° C. as measured according to ASTM D6352;', 'a pour point of ≤about 0.0° C., as measured according to ASTM D7346; and', {'sup': 2', '2, 'a kinematic viscosity at 50° C. from 20 mm/s to 200 mm/s, as measured according to ASTM D7042.'}], 'wherein the first hydroprocessed product has2. The first hydroprocessed product of further comprising asphaltenes in an amount from about 2.0 wt % to 10 wt %.3. The first hydroprocessed product of claim 1 , wherein the aromatics are present in an amount of ≥about 80 wt %.5. The first hydroprocessed product of having a pour point of ≤−5.0° C. claim 1 , as measured according to ASTM D7346.6. The first hydroprocessed product of having one or more of the following:(i) a Bureau of Mines Correlation Index (BMCI) of ≥about 100;{'sub': 'n', '(ii) a solubility number (S) of ≥about 130; and'}(iii) an energy content of ≥about 35 MJ/kg.7. A second hydroprocessed product comprising:aromatics in an amount ≥about 50 wt %;paraffins in an amount ≤about 5.0 wt %; andsulfur in an amount ≤0.30 wt %; a boiling point distribution of about 140° C. to about 760° C. as measured according to ASTM D6352;', 'a pour point of ≤about 12° C., as measured according to ASTM D5949; and', {'sup': 2', '2, 'a kinematic viscosity at 50° C. from 100 mm/s to 800 mm/s, as measured according to ASTM D7042.'}], ' ...

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Номер записи: 80
16-01-2020 дата публикации

PROCESS FOR PRODUCING HYDROCARBONS

Номер: US20200017775A1
Автор: BJÖRKLÖF Thomas, Eilos Isto, LINDBERG Teemu
Принадлежит:

The present invention relates to a process for producing hydrocarbons, said process comprising the steps, where feedstock of biological origin is degummed, the degummed feedstock is subjected to bleaching and/or hydrolysis, followed by hydroprocessing and catalytic cracking. 1. A process for producing hydrocarbons , where said process comprises the steps ,feedstock of biological origin is degummed to produce degummed feedstock;the degummed feedstock is subjected to bleaching and/or hydrolysis to produce pretreated feedstock;the pretreated feedstock is hydroprocessed catalytically to produce hydroprocessed feedstock;the hydroprocessed feedstock is fractionated to produce at least one fraction comprising hydrocarbons having carbon number of at least C20; andthe fraction comprising hydrocarbons having carbon number of at least C20 andat least one non-renewable feedstock is subjected to catalytic cracking to produce a product comprising hydrocarbons boiling in the range of 40-210° C.,wherein the feedstock of biological origin comprises at least one oil derived from biological sources, comprising at least 85 wt % of C18-C26 fatty acids, wherein the C18-C26 fatty acids comprise at least 30 wt % of C20-C26 fatty acids.2. The process according to claim 1 , wherein the fraction comprising hydrocarbons having carbon number of at least C20 is combined with the non-renewable feedstock.3. The process according to claim 1 , wherein the feedstock of biological origin comprises at least one oil derived from biological sources claim 1 , comprising at least 85-99 w % of C18-C26 fatty acids.4. The process according to claim 3 , wherein the C18-C26 fatty acids comprise 30-60 wt % of C20-C26 fatty acids.5Brassica. The process according to claim 1 , wherein the feedstock of biological origin comprises at least one plant oil originating from species.6Brassica. The process according to claim 1 , wherein the feedstock of biological origin is selected from mixtures of plant oil(s) claim 1 , ...

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Номер записи: 81
21-01-2021 дата публикации

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Номер: US20210017458A1
Автор: Pruitt Tom F., Wohaibi Mohammed
Принадлежит: MAWETAL LLC

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or CS to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 129-. (canceled)30. A fuel derived from combining(a) light oil and (1) said unconverted oils passed to solvent separation to remove insoluble remaining metals and asphaltenes to form soluble deasphalted oil, and', (i) an actual sulfur content of 0.5 wt. % or less, and', '(ii) initial boiling point being that of lowest boiling component of light tight oil or lighter materials from said hydroconversion so combined and', '(iii) highest boiling point being that of highest boiling component of said treated soluble deasphalted oil derived from high sulfur fuel oil or other residuals so combined., '(2) said soluble deasphalted oil subsequent treated either by additional hydrotreating or additional hydroconversion to form said treated soluble deasphalted oil, said fuel having'}], '(b) hydroconversion reaction effluent comprising treated soluble deasphalted oil and lighter materials derived from hydroconversion of high sulfur fuel oil, or other residuals processed by residue hydroconversion to form said effluent comprising treated liquids and unconverted oils,'}3150-. (canceled)51. A fuel characterized by comprising:(a) all or a portion of a ...

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Номер записи: 82
21-01-2021 дата публикации

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Номер: US20210017459A1
Автор: Pruitt Tom F., Wohaibi Mohammed
Принадлежит: MAWETAL LLC

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 1. A process for conversion of hydrocarbonaeous feeds comprising sulfur and metals to form a fuel characterized in that feed comprises light tight oil and high sulfur fuel oil , said process comprising{'b': 41', '401, 'claim-text': [{'b': 411', '420, '(1) reactor zone effluent which is separated into hydroconverted liquids () and purge gases () comprising hydrogen and sulfur,'}, {'b': 409', '301', '311', '401', '351', '501, '(2) unconverted oils () which are directed to solvent separation () to form (A) soluble deasphalted oil () which is recycled as feed to said hydroconversion zone (), either separately or combined with added high sulfur fuel oil feed to said reactor and (B) insoluble pitch () which is directed to pitch treatment (), and'}], '(a) feeding one or more high sulfur fuel oils () to a residue hydroconversion zone () and contacting such oil with hydrogen in presence of catalyst at residue hydroconversion conditions in an ebullated-bed reactor to form'}{'b': 1', '411', '600, '(b) combining all or one or more portions of a light tight oil () with said hydroconverted liquids () to form a fuel ().'}2. A process in accordance ...

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Номер записи: 83
21-01-2021 дата публикации

Fuel compositions from light tight oils and high sulfur fuel oils

Номер: US20210017460A1
Автор: Mohammed Wohaibi, Tom F. Pruitt
Принадлежит: MAWETAL LLC

Methods are provided to prepare a low sulfur fuel from hydro-carbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains.

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Номер записи: 84
21-01-2021 дата публикации

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Номер: US20210017461A1
Автор: Pruitt Tom F., Wohaibi Mohammed
Принадлежит: MAWETAL LLC

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 144-. (canceled)45. A formulated combination useful as a fuel characterized in that it is formed by combining a range of hydrocarbons of (L)+(M)+(H) and the resulting combination is from 30% to 70% by volume of (M) range constituents and the remainder is equal parts of (L) and (H) at (L)/(H) in ratio of 0.9/1 to 1/0.9 , for 100 volume percent total , and final combination density is within 820 to 880 Kg/M3 at 15° C. , total sulfur is 0.25 wt. % or less and metals are 40 ppmwt or less(a) wherein (L) comprises components of naphtha and kerosene range materials, which are refined or partially refined, unrefined or extracted and used without being subject to any fractionation, hydrotreating or other treatment process, except optional separation of light gases or water, having an initial boiling point of 38° C. (100° F.) or less having a ninety percent (90%) plus final boiling point of 190° C. (374° F.) to about 205° C. (401° F.), where (L) range components contribute to (L) range bulk density and to final combination density even though individual constituents of (L) may fall outside said combination density range(b) wherein (M) ...

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Номер записи: 85
16-01-2020 дата публикации

PROCESS FOR SELECTIVELY RECOVERING A PHENOLIC COMPOUND FROM FEEDSTOCK COMPRISING BIO-CRUDE AND/OR BIO-OIL

Номер: US20200017778A1
Автор: Dayton David C., Mante Ofei D., SOUKRI Mustapha, Thompson Samuel J.
Принадлежит:

A process for selectively recovering a phenolic compound from feedstock comprising bio-crude and/or bio-oil is described. The recovery efficiency of the selected phenolic compound is greater than 70 wt % and the purity of the recovered selected phenolic compound is higher than 80 wt %. The process comprises distilling the feedstock to isolate the selected phenolic compound in a first distillate fraction comprising the selected phenolic compound, concentrating the selected phenolic compound from the first distillate fraction in a concentrated mixture, and purifying the concentrated mixture to recover the selected phenolic compound. 1. A process for selectively recovering a phenolic compound from feedstock comprising bio-crude and/or bio-oil , wherein the recovery efficiency of the selected phenolic compound is greater than 70 wt % and the purity of the recovered selected phenolic compound is higher than 80 wt % , the process comprising:distilling the feedstock to isolate the selected phenolic compound in a first distillate fraction comprising the selected phenolic compound,concentrating the selected phenolic compound from the first distillate fraction in a concentrated mixture, andpurifying the concentrated mixture to recover the selected phenolic compound.2. The process of claim 1 , wherein concentrating comprises using solvent extraction to concentrate the selected phenolic compound in a concentrated mixture.3. The process of claim 2 , wherein extracting the selected phenolic compound from the first distillate fraction comprises adjusting the pH of the first distillate fraction based on the pKa of the selected phenolic compound prior to extraction.4. The process of claim 3 , wherein the pH of the first distillate fraction is adjusted by adding an acid solution and/or a base solution thereto.5. The process of claim 2 , wherein extracting comprises sequential extraction at decreasing pH levels.6. The process of claim 5 , wherein sequential extraction comprises ...

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Номер записи: 86
22-01-2015 дата публикации

SEQUENTIAL SLURRY HYDROCONVERSION OF HEAVY OILS

Номер: US20150021233A1
Автор: Billimoria Rustom Merwan, Degnan, JR. Thomas Francis, Smiley Randolph J., Sundararaman Ramanathan
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Systems and methods are provided for sequential slurry hydroconversion of heavy oil feedstocks. One or more low pressure slurry hydroconversion stages can be used to perform a majority of the conversion of a heavy oil feedstock. The bottoms from the low pressure stages can then be slurry hydroconverted in one or more high pressure stages to further convert the feedstock. 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.);exposing the heavy oil feedstock to a catalyst under first effective slurry hydroconversion conditions to form an effluent comprising at least a plurality of liquid products and a bottoms product, the first effective slurry hydroconversion conditions comprising a hydrogen partial pressure of about 1500 psig (10.3 MPag) or less, optionally about 1000 psig (6.9 MPag) or less, optionally about 500 psig (3.4 MPag) or less;exposing at least a portion of the bottoms product to the catalyst under second effective slurry hydroconversion conditions to form at least a second plurality of liquid products and a second bottoms product; andrecycling at least a portion of the second bottoms product, the recycled portion of the second bottoms product being combined with the heavy oil feedstock prior to exposing the heavy oil feedstock under the first slurry hydroconversion conditions.2. 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.);exposing the heavy oil feedstock to a catalyst under first effective slurry hydroconversion conditions to form an effluent comprising at least a plurality of liquid products and a bottoms product, the first effective slurry hydroconversion conditions comprising a hydrogen partial pressure of about 1500 psig (10.3 MPag) or less;exposing at least a portion of the bottoms product to a second catalyst under second ...

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Номер записи: 87
26-01-2017 дата публикации

Catalyst Reactor Basket

Номер: US20170021320A1
Автор: Al-Khaldi Salman J., KOSEOGLU Omer Refa
Принадлежит: Saudi Arabian Oil Company

A catalyst reactor basket is provided that includes an outer side wall extending along the outer circumferential periphery and an inner side wall disposed within the outer side wall. An aperture is sized and shaped to allow a fluid to flow axially with respect to the basket. First and second covers are disposed on opposite ends of the outer side wall and inner side wall and a dividing wall is disposed between the first and second covers. The dividing wall defines a first and second chamber within the inner volume of the basket. A plurality of partitions are disposed within the first and second chambers. The plurality of partitions define a plurality of compartments within the first and second chambers, each compartment being sized and shaped to receive a catalyst. 111-. (canceled)12. A catalyst reactor basket arranged to receive a combination of catalysts in separate chambers , comprising:an outer side wall extending along the outer periphery of the basket and extending to define an inner volume of the basket;an inner side wall disposed within the outer side wall, the inner side wall extending to define an aperture that defines a inner boundary of the volume of the basket, the aperture being sized and shaped to allow a fluid to flow axially with respect to the basket;first and second covers disposed on opposite ends of the outer side wall and inner side wall, the first and second covers defining respective ends of the inner volume of the basket, at least a portion of the first and second covers being fluid permeable; anda dividing wall disposed between the first and second covers, the dividing wall defining a first and second chamber within the inner volume of the basket, at least a portion of the dividing wall being fluid permeable, wherein each of the first and second chambers being sized to receive a respective catalyst so as to enable a two-stage reaction in a single pass of the fluid in the axial direction.13. The catalyst reactor basket as in claim 12 , ...

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Номер записи: 88
26-01-2017 дата публикации

PROCESS FOR IMPROVING COLD FLOW PROPERTIES AND INCREASING YIELD OF MIDDLE DISTILLATE FEEDSTOCK THROUGH LIQUID FULL HYDROTREATING AND DEWAXING

Номер: US20170022432A1
Автор: BOEGER BRIAN, Dindi Hasan, Murillo Luis Eduardo, PALIT SANDEEP, Pulley Alan Howard, Ta Thanh Gia
Принадлежит:

Novel liquid-full process for improving cold flow properties and increasing yield of middle distillate fuel feedstock by hydrotreating and dewaxing the feedstock in liquid-full reactors. 2. The process of claim 1 , wherein the middle distillate fuel feedstock has a nitrogen content of at least 200 wppm claim 1 , and the middle distillate product has a cloud point of at least 15° C. lower compared to the middle distillate fuel feedstock.3. The process of claim 1 , wherein the middle distillate fuel feedstock has a nitrogen content of at least 90 wppm claim 1 , and the middle distillate product has a cloud point of at least 25° C. lower compared to the middle distillate fuel feedstock.4. The process of claim 1 , wherein steps (b) and (c) are conducted in a single reactor containing one or more catalyst beds.5. The process of claim 1 , wherein steps (b) and (c) are conducted in separate reactors claim 1 , each of the reactors containing one or more catalyst beds.6. The process of claim 1 , wherein the first product effluent includes HS and NHdissolved therein and is fed directly into the second reaction zone without separating ammonia claim 1 , hydrogen sulfide and remaining hydrogen from the first product effluent.7. The process of claim 1 , wherein the first reaction zone has a temperature in the range of about 225° C. to about 425° C. and a pressure in the range of about 3.0 MPa to about 17.5 MPa.8. The process of claim 1 , wherein the second reaction zone has a temperature in the range of about 225° C. to about 425° C. and a pressure in the range of about 3.0 MPa to about 17.5 MPa.9. The process of claim 1 , wherein both the middle distillate fuel feedstock and the middle distillate product are diesels.10. The process of claim 1 , wherein the dewaxing catalyst is selected from the group consisting of catalysts comprising a non-precious metal and an oxide support claim 1 , catalysts comprising a crystalline claim 1 , microporous oxide structure without metal loaded ...

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Номер записи: 89
25-01-2018 дата публикации

METHOD FOR SOFTENING SULFIDE-TYPE COMPOUNDS OF AN OLEFINIC GASOLINE

Номер: US20180023010A1
Автор: ASTERIS Diamantis, GARCIA-LOPEZ Clementina, GODARD-PITHON Marie, GORNAY Julien, LEFLAIVE Philibert, PUCCI Annick
Принадлежит: IFP ENERGIES NOUVELLES

This invention relates to a method for reducing the content of sulfide-type compounds of formula R1-S—R2, with R1 and R2 selected from among the methyl (CH) and ethyl (CH) radicals, of a gasoline that contains diolefins, monoolefins, and sulfur. The method implements a first catalytic step for selective hydrogenation of diolefins at a temperature of between 60° C. and 150° C. and then a step for heating the effluent that is obtained from the first step with a temperature difference ΔT of between 10° C. and 100° C. and a second catalytic step on the effluent that is heated in such a way as to produce an effluent that has a content of sulfide-type compounds of formula R1-S—R2, with R1 and R2 selected from among the methyl (CH3) and ethyl (C2H5) radicals, lower than that of the starting gasoline. 1. Method for reducing the content of sulfide-type compounds of formula R1-S—R2 , with R1 and R2 selected from among the methyl (CH) and ethyl (CH) radicals , of a gasoline that contains diolefins , monoolefins , and sulfur , in which:{'sup': '−1', 'claim-text': {'sup': '−1', 'sub': '2', '10 h, a pressure of between 0.5 and 5 MPa, and with a volumetric ratio of added H/gasoline feedstock of between 1 to 40 normal liters of hydrogen per liter of gasoline (vol/vol), in such a way as to produce an effluent at a temperature T1 of between 60° C. and 150° C. and having a lower diolefin content than that of the starting gasoline;'}, 'A) In a first reactor, the gasoline is brought into contact with hydrogen and a catalyst A that comprises at least one metal of group VIb and at least one non-noble metal of group VIII that are deposited on a substrate, with step A being carried out at a temperature in the reactor of between 60° C. and 150° C. with an hourly volumetric flow rate (VVH) of between 1 hand'}B) The effluent that is obtained from the first reactor is heated in a heating device at a temperature T2 with a temperature difference ΔT (T2-T1) of between 10° C. and 100° C.; {'sup': − ...

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Номер записи: 90
10-02-2022 дата публикации

PROCESS FOR INTEGRATED PRODUCTION OF RENEWABLE FUELS AND CHEMICALS

Номер: US20220041939A1
Автор: MYLLYOJA Jukka, SIPPOLA Väinö, Tiitta Marja
Принадлежит: Neste Oyj

The present disclosure provides a versatile process for producing valuable renewable hydrocarbons from triglyceride containing feedstock. The triglyceride containing feedstock is first split to provide a mixture containing fatty acids, glycerol and water, from which a phase separation provides an oily phase, and an aqueous phase. The oily phase containing fatty acids is subjected to fractionation, whereby specific fractions may be refined to products with controlled hydroprocessing. Products may contain paraffinic renewable aviation fuel components, paraffinic renewable base oil, renewable paraffinic diesel fuel components, renewable paraffinic technical fluid, or any combination thereof. 1. A process for producing renewable hydrocarbon components from triglyceride containing feedstock , said process comprising:a. hydrolyzing said triglyceride containing feedstock to provide a mixture containing at least one or more of fatty acids, glycerol and water;b. subjecting said mixture comprising containing at least one or more of fatty acids, glycerol and water to a phase separation to recover an oily phase containing fatty acids, and an aqueous phase containing glycerol and water;c. subjecting said oily phase containing fatty acids to fractionation to provide a first fatty acid fraction containing at least 80%-wt of free fatty acids having a carbon chain length of C16 or less, of a total fraction weight, and a second fatty acid fraction containing free fatty acids having a carbon chain length of at least C17; hydroprocessing to provide a paraffinic renewable aviation fuel component, or', 'ketonisation before hydroprocessing to provide a paraffinic renewable base oil, or', 'a combination thereof;, 'd. subjecting said first fatty acid fraction to a renewable paraffinic diesel fuel component, or', 'a renewable paraffinic technical fluid, or', 'a combination thereof; and, 'e. subjecting said second fatty acid fraction to hydroprocessing to providef. recovering renewable ...

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Номер записи: 91
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: 92
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: 93
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: 94
29-01-2015 дата публикации

LUBRICANT BASE OIL HYDROPROCESSING AND BLENDING

Номер: US20150027925A1
Автор: Berberich Sara M., Carroll Michael Brian, Joseck Eric D., Mentzer David, Shukla Yogi V.
Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Methods are provided for producing a plurality of lubricant base oil products with an increased overall yield. Prior to the final hydrocracking stage for viscosity index uplift, a feed for making a lubricant base oil is fractionated in order to form at least a feed for making a lighter lubricant base oil and a feed for making a heavier lubricant base oil. The fractionation cut points are selected to so that the feed fraction for forming a light lubricant base oil has a higher Noack volatility and a lower viscosity than the desired targets for the lighter lubricant base oil. The feed fractions are then hydroprocessed separately to achieve desired properties. After hydroprocessing, a portion of the heavier base oil is blended into the light lubricant base oil to produce a blended base oil product. This returns the volatility and the viscosity of the blended base oil to the desired specifications. 1. A method for producing a lubricant base oil , comprising:fractionating a feedstock to form at least a first feed fraction and a second feed fraction;hydroprocessing the first feed fraction to increase the viscosity index to at least about 85 and reduce the pour point to about −10° C. or less;hydroprocessing the second feed fraction to increase the viscosity index to at least about 80 and reduce the pour point to about −5° C. or less;fractionating the hydroprocessed first feed fraction to form a first product fraction having a viscosity at 100° C. of at least about 1.5 cSt and a Noack volatility of less than about 20.0;fractionating the hydroprocessed second feed fraction to form a second product fraction having a viscosity at 100° C. of about 5.0 cSt to about 12.0 cSt and a Noack volatility of about 5.0 to about 10.0; andblending a portion of the second hydroprocessed feed fraction with the first hydroprocessed feed fraction to form a blended product fraction, the second hydroprocessed feed fraction comprising about 30 wt % or less of the blended product fraction, the ...

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Номер записи: 95
28-01-2021 дата публикации

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Номер: US20210024838A1
Автор: Pruitt Tom F., Wohaibi Mohammed
Принадлежит: MAWETAL LLC

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 115-. (canceled)16. A process for conversion of one or more hydrocarbonaeous feeds comprising sulfur and metals characterized in that said conversion is directed to a single liquid fuel product , said process comprising{'b': 2', '3', '100', '200, 'claim-text': [{'b': '6', '(i) light overhead still gases (),'}, {'b': '16', '(ii) liquid fractions at or below sulfur breakpoint (), and'}, [{'b': 24', '26', '28', '32, '(A) distillate range fractions comprising sulfur (,,, )'}, {'b': 36', '38, '(B) vacuum gas oil range fractions comprising sulfur (, ) and'}, {'b': '50', '(C) vacuum residue comprising sulfur (), and associated purge gases comprising sulfur'}], '(iii) fractions above sulfur breakpoint comprising'}], '(a) separating said feed (, ) by atmospheric () and vacuum distillation (), into'}{'b': 10', '600, '(b) directing the liquid fractions at or below the sulfur breakpoint (), as untreated liquids, to a combination zone ()'}{'b': 16', '20', '430', '16', '39', '460, 'claim-text': [{'b': 65', '75', '600, '(1) one or more treated liquids (, ) which are directed to a combination zone (), and'}, {'b': '428', '(2) purge gases comprising ...

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Номер записи: 96
28-01-2021 дата публикации

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Номер: US20210024839A1
Автор: Pruitt Tom F., Wohaibi Mohammed
Принадлежит: MAWETAL LLC

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired FIG. by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 114-. (canceled)15. Combustion in marine or land based engines , combustion gas turbines , or fired heaters of a fuel comprising light tight oil and processed high sulfur fuel oil , wherein{'b': 41', '401, 'claim-text': [{'b': '411', '(1) hydroconverted liquids () and'}, {'b': 409', '301', '311', '401, '(2) unconverted oils () directed to solvent separation () to form soluble deasphalted oil () for recycle as feed to said hydroconversion zone (), either separately or combined with added high sulfur fuel oil feed to said reactor and'}], '(a) said processed high sulfur fuel oil () has been processed in a residue hydroconversion zone () by contact with hydrogen in presence of catalyst at residue hydroconversion conditions in an ebullated-bed reactor to form'}{'b': 1', '15, 'i': 'a', '(b) all or one or more portions of a light tight oil () is combined with said processed high sulfur fuel oil of .() to form said fuel.'}1628-. (canceled)29. Combustion in marine or land based engines , combustion gas turbines , or fired heaters of a single fuel product of one or more hydrocarbonaeous feeds comprising sulfur and metals , said fuel ...

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Номер записи: 97
28-01-2021 дата публикации

FUEL COMPOSITIONS FROM LIGHT TIGHT OILS AND HIGH SULFUR FUEL OILS

Номер: US20210024840A1
Автор: Pruitt Tom F., Wohaibi Mohammed
Принадлежит: MAWETAL LLC

Methods are provided to prepare a low sulfur fuel from hydrocarbon sources, such as light tight oil and high sulfur fuel oil, often less desired by conventional refiners, who split crude into a wide range of differing products and may prefer presence of wide ranges (C3 or C5 to C20 or higher) of hydrocarbons. These fuels can be produced by separating feeds into untreated and treated streams, and then recombining them. Such fuels can also be formulated by combinations of light, middle and heavy range constituents in a selected manner as claimed. Not only low in sulfur, the fuels of this invention are also low in nitrogen and essentially metals free. Fuel use applications include on-board large marine transport vessels but also on-shore for large land based combustion gas turbines, boilers, fired heaters and transport vehicles and trains. 147-. (canceled)48. A formulated combination useful as a fuel characterized in that it is formed by combining a range of hydrocarbons of (L)+(M)+(H) and the resulting final combination has the following properties:(a) sulfur from 0.05 wt. % (500 ppmwt) to 0.25 wt. % (2500 ppmwt),(b) final combination density from 820 to 880 Kg/M3 at 15° C.,(c) total metals of 25 ppmwt or less,(d) HHV from 43.81 to 45.15 MJ/kg, and(e) LHV from 41.06 to 42.33 MJ/kgwherein,(f) wherein (L) comprises components of naphtha and kerosene range materials, which are refined or partially refined, unrefined or extracted and used without being subject to any fractionation, hydrotreating or other treatment process, except optional separation of light gases or water, having an initial boiling point of 38° C. (100° F.) or less having a ninety percent (90%) plus final boiling point of 190° C. (374° F.) to about 205° C. (401° F.), where (L) range components contribute to (L) range bulk density and to final combination density even though individual constituents of (L) may fall outside said combination density range(g) wherein (M) comprises refined or partially refined ...

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Номер записи: 98
02-02-2017 дата публикации

Process and Apparatus for Recovering Aromatic Hydrocarbons

Номер: US20170029348A1
Автор: Timothy P. Bender
Принадлежит: ExxonMobil Chemical Patents Inc

The present invention relates to an improved extractive distillation process for recovering aromatic hydrocarbons from non-aromatic hydrocarbons in naphtha streams containing heavy hydrocarbon contaminants wherein each contaminant is characterized as having a boiling point in the range of between that of the separated non-aromatic hydrocarbons and the extractive distillation solvent utilized to recover and purify the aromatic hydrocarbons.

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Номер записи: 99
02-02-2017 дата публикации

OPTIMISATION OF THE USE OF HYDROGEN FOR HYDROTREATMENT OF HYDROCARBON FEEDSTOCKS

Номер: US20170029717A1
Автор: Lecocq Vincent, PIERRON Anne Claire, PLENNEVAUX Thomas
Принадлежит: IFP ENERGIES NOUVELLES

A process for the hydrotreatment of a hydrocarbon feedstock in which: 1. A process for the hydrotreatment of a hydrocarbon feedstock comprising sulphurous and nitrogenous compounds , in which the following steps are effected:{'b': 9', '400, 'a) at least one hydrotreatment step is implemented in which at least a part of said feedstock and a gaseous flow comprising hydrogen is brought into contact with at least one hydrotreatment catalyst to obtain a hydrotreated effluent (,) comprising hydrogen, and sulphurous and nitrogenous compounds;'}{'b': 9', '400', '23', '240', '11', '600, 'b) gas/liquid separation of said hydrotreated effluent (,) obtained in step a) is implemented to produce at least one first gaseous effluent (,) and at least one first liquid effluent (,);'}{'b': 11', '600', '11', '600', '41', '410', '43', '430, 'c) the first liquid effluent (,) obtained in step b) is expanded to a pressure of between 0.5 and 4 MPa and said first liquid effluent (,) is separated to obtain at least one second gaseous effluent (,) comprising hydrogen and sulphurous and nitrogenous compounds, and at least one second liquid effluent (,);'}{'b': 41', '410', '41', '410', '49', '490', '45', '450, 'd) said second gaseous effluent (,) obtained in step c) and comprising hydrogen and sulphurous and nitrogenous compounds is cooled and then separation of said second gaseous effluent (,) is effected to obtain at least one third gaseous effluent (,) comprising hydrogen, sulphurous and nitrogenous compounds and at least one third liquid effluent (,); and'}{'b': 49', '490, 'e) at least a part of said third gaseous effluent (,) obtained in step d) comprising hydrogen and sulphurous and nitrogenous compounds is recycled to step a) as a gaseous flow comprising hydrogen provided to step a).'}230301. A process according to characterised in that in step e) said part of said third gaseous effluent is mixed with a gaseous hydrogen make-up flow ( claim 1 ,).3. A process according to characterised in ...

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Номер записи: 100