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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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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

27-05-2004 дата публикации

СИСТЕМА МНОГОКРАТНОГО ИСПОЛЬЗОВАНИЯ ПРОМЫВНОЙ ВОДЫ ПРИ ОБЕССОЛИВАНИИ КОНДЕНСАТА

Номер: RU0000038168U1

Автор: Арабов М.Ш., Мухаммадиев Р.Т., Солодкий А.М.

Принадлежит: Арабов Михаил Шугеевич, Мухаммадиев Рубин Таштимирович, Солодкий Анатолий Михайлович

Система многократного использования промывной воды при обессоливании конденсата, состоящая из трубопровода нестабильного конденсата, трубопровода с установки фильтрации пластовой воды, трубопровода деминерализованной воды, буферной емкости, электрообессоливателя, трубопровода обессоленного нестабильного конденсата, трубопровода дренируемой пластовой воды, трубопровода на установку фильтрации пластовой воды, трубопровода соляной кислоты HCl, трубопровода щелочи NaOH, емкость-сепаратора пластовой воды и углеводородов, емкость-реактора, емкость-нейтрализатора, трубопровода утилизированной пластовой воды, трубопровода деэмульгатора, трубопровода стабильного конденсата, дегидратора первой ступени, дегидратора второй ступени, трубопровода подготовленного конденсата, трубопровода пресной промывной воды, трубопровода пластовой промывной воды, причем буферная емкость соединена трубопроводом с электрообессоливателем, а емкость-сепаратор пластовой воды и углеводородов трубопроводом соединена с емкостью-реактором, при этом емкость-реактор трубопроводом соединена с емкость-нейтрализатором, а дегидратор первой и второй ступени соединяются трубопроводом, дегидратор второй ступени соединен трубопроводом с трубопроводом стабильного конденсата, отличающаяся тем, что в нее введены, трубопровод промывной воды с деэмульгатором, заглушка в трубопровод деминерализованной воды, заглушка в трубопровод пластовой промывной воды, причем трубопровод промывной воды с деэмульгатором монтируется между трубопроводом промывной воды и трубопроводом деминерализованной воды, при этом трубопровод промывной водой с деэмульгатором монтируется после заглушки на трубопроводе деминерализованной воды перед буферной емкостью, но перед заглушкой трубопровода пластовой промывной воды. (19) RU (11) 38 168 (13) U1 (51) МПК C10G 63/00 (2000.01) C10G 59/02 (2000.01) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ПОЛЕЗНОЙ МОДЕЛИ К ПАТЕНТУ (21), (22) Заявка: 2004104643/20 , 16.02.2004 (24) Дата ...

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Номер записи: 2

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: 3

26-01-2012 дата публикации

Methods for deoxygenating biomass-derived pyrolysis oils

Номер: US20120017495A1

Автор: Jennifer F. ABRAHAMIAN, Thomas Traynor, Timothy A. Brandvold

Принадлежит: UOP LLC

Methods for deoxygenating treated biomass-derived pyrolysis oil are provided. The treated biomass-derived pyrolysis oil is exposed to a catalyst having a neutral catalyst support such as a non-alumina metal oxide support, a theta alumina support, or both. The non-alumina metal oxide support may be a titanium oxide (TiO 2 ) support, a silicon oxide support, a zirconia oxide (ZrO 2 ) support, a niobium oxide (Nb 2 O 5 ) support, or a support having a mixture of non-alumina metal oxides. The catalyst may include a noble metal or a Group VIII non-noble metal and a Group VIB non-noble metal on the neutral catalyst support. The treated biomass-derived pyrolysis oil is introduced into a hydroprocessing reactor in the presence of the catalyst under hydroprocessing conditions to produce low oxygen biomass-derived pyrolysis oil.

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Номер записи: 4

01-03-2012 дата публикации

Dimethyl ether fuel compositions and uses thereof

Номер: US20120047796A1

Автор: David Aldous, Ronald C. Stites

Принадлежит: Range Fuels Inc

The present invention provides useful fuel compositions which may be produced substantially from renewable resources, such as biomass, to provide green fuel compositions, methods, and systems. In some embodiments, fuel compositions include dimethyl ether and one or more C 2 or larger alcohol, such as ethanol, 1-propanol, 2-propanol, 1-butanol, 2-butanol, isobutanol, or tert-butanol. In some embodiments, fuel compositions include dimethyl ether and one or more C 2 or larger hydrocarbons, such as propane, propylene, propyne, and propadiene, n-butane, isobutane, isobutylene, 1-butene, 2-butene, or 1,3-butadiene. Methods of making these novel DME-based fuel compositions, particularly from biomass-derived syngas, are described. Various applications and methods of using the fuel compositions, such as portable cylinder fuels for camping, are disclosed. Additionally, principles of burner design for these fuel compositions are disclosed herein.

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Номер записи: 5

15-03-2012 дата публикации

Oligomerization of propylene and longer chain alpha olefins to produce base oil products

Номер: US20120065448A1

Автор: Saleh Elomari, Stephen Joseph Miller

Принадлежит: Chevron USA Inc

We provide a process for making a base oil, comprising: mixing one or more longer chain alpha olefins comprising C6+ olefins with an olefin feed comprising propylene to make a mixed olefin feed; and oligomerizing the mixed olefin feed using an acidic chloroaluminate ionic liquid catalyst to form an oligomer; wherein the oligomer is a base oil that has: i. a kinematic viscosity at 100° C. greater than 10 mm 2 /s; ii. a viscosity index from 50 to 90; iii. a pour point less than −19° C.; and iv. a cloud point less than −50° C.

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Номер записи: 6

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: 7

24-05-2012 дата публикации

Process for Cracking Heavy Hydrocarbon Feed

Номер: US20120125812A1

Автор: Robert S. Bridges, Sellamuthu G. Chellappan

Принадлежит: EQUISTAR CHEMICALS LP

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

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Номер записи: 8

31-05-2012 дата публикации

Methods for producing fuels and solvents

Номер: US20120136185A1

Автор: David Bressler

Принадлежит: University of Alberta

Described herein are methods for producing fuels and solvents from fatty acid resources. Also disclosed herein are fuels and solvents produced by the methods described herein.

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Номер записи: 9

07-06-2012 дата публикации

Process to produce low sulfur catalytically cracked gasoline without saturation of olefinic compounds

Номер: US20120138510A1

Автор: Ali H. Al-Shareef, Ki-Hyouk Choi, Sameer A. Al-Ghamdi

Принадлежит: Saudi Arabian Oil Co

The invention relates to a process for the desulfurization of a gasoline fraction with high recovery of olefins and reduced loss of Research Octane Number (RON). A petroleum fraction is contacted with hydrogen and a commercially available hydrodesulfurization catalyst under mild conditions with to remove a first portion of the sulfur present, and is then contacted with an adsorbent for the removal of additional sulfur.

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Номер записи: 10

02-08-2012 дата публикации

Composition of matter comprising of the creation of a low molecular weight hydrocarbon fluid exhibiting oligomerized pentenes mainly comprised of 2-Methyl-2-Butene subunits as well as related plant isoprenoids composed of 2-Methyl-1-Butene subunits and other hydrocarbons from hydrocarbon-bearing woody biomass and a process for the extraction and refinement in making the same composition through the creation of solvent permeable woody biomass particles and a multi-phase solvent extraction

Номер: US20120197049A1

Автор: Stephen Daniel Matthews

Принадлежит: Individual

A composition of matter with of the creation of a low molecular weight hydrocarbon fluid called Wood Phytoleum from woody Pinaceae and Myrtaceae biomass and a process for the extraction and refinement in making the same composition of matter through the reduction of the particle size of the raw woody biomass to form a solvent permeable particle and a phased multi-wash solvent system of extraction and refinement. A preferred embodiment includes the steps of the reduction of the particle size of the raw woody biomass to form a solvent permeable particle by shearing and chipping, the application of a phased multi-wash solvent system to the solvent permeable particle utilizing a non-polar solvent together with a bridge solvent soluble in both the non-polar solvent and in water, the application of a final bridge solvent wash to the solvent permeable particle, a mechanism for washing the particles of the woody biomass within the multi-wash solvent system, a mechanism for the collection of the solvent and Wood Phytoleum solution from the multi-wash solvent system, the extraction of the solvent from the solvent saturated particles of the woody biomass and the discharge for continued use of the woody biomass, and a process and mechanism for the extraction, collection and refinement of the solvent and Wood Phytoleum solution to discharge the solvents for reuse and to collect the Wood Phytoleum liquid oil including Pinene A and Pinene B and other oligomerized pentenes.

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Номер записи: 11

02-08-2012 дата публикации

Composition of matter comprising of the creation of a low molecular weight hydrocarbon fluid exhibiting mainly oligomerized pentenes mainly comprised of 2-Methyl-2-Butene subunits as well as related plant isoprenoids composed of 2-Methyl-1-Butene subunits and other hydrocarbons from Euphorbia tirucalli biomass and a process for the extraction and refinement in making the same composition through the creation of solvent permeable batting mat and a multi-phase solvent extraction

Номер: US20120197052A1

Автор: Stephen Daniel Matthews

Принадлежит: Individual

A composition of matter with of the creation of low molecular weight hydrocarbon fluid called Phytoleum from Euphorbia tirucalli biomass and a process for the extraction and refinement in making the same composition through the creation of a batting mat and multi-phase solvent extraction. A preferred embodiment includes the steps of manufacturing a fibrous batting mat from the raw biomass, crushing the biomass, shearing the biomass with a rotating knives blade array, compressing the biomass by passing the biomass through press rollers, amalgonating the biomass into a Batting Mat, subjecting the Batting Mat to a phased multi-wash solvent system, extracting the solvents and oils liquid solution for recovery, subjecting the liquid solution to a centrifugation system to extract the Phytoleum hydrocarbon oil from the other components, and refining the final product to yield Phytoleum which is a composition of matter including Tirucallene A and Tirucallene B and other oligomerized pentenes.

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Номер записи: 12

09-08-2012 дата публикации

Method and systems for making distillate fuels from biomass

Номер: US20120198760A1

Автор: Brice Dally, Paul Blommel, Randy CORTRIGHT, Warren Lyman

Принадлежит: Brice Dally, Paul Blommel, Randy CORTRIGHT, Warren Lyman

The present invention provides methods, reactor systems and catalysts for converting biomass and biomass-derived feedstocks to C 8+ hydrocarbons using heterogenous catalysts. The product stream may be separated and further processed for use in chemical applications, or as a neat fuel or a blending component in jet fuel and diesel fuel, or as heavy oils for lubricant and/or fuel oil applications.

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Номер записи: 13

09-08-2012 дата публикации

Production of hydrocarbons

Номер: US20120202899A1

Автор: Abdool Muthalib Saib, Herman Preston, Jacobus Lucas Visagie

Принадлежит: Sasol Technology Pty Ltd

A process for producing hydrocarbons and, optionally, oxygenates of hydrocarbons is provided. A synthesis gas comprises hydrogen, carbon monoxide and N-containing contaminants selected from the group consisting of HCN, NH 3 , NO, R X NH 3-X , R 1 —CN and heterocyclic compounds containing at least one nitrogen atom as a ring member of a heterocyclic ring of the heterocyclic compound. The N-containing contaminants constitute, in total, at least 100 vppb but less than 1 000 000 vppb of the synthesis gas. The synthesis gas is contacted at an elevated temperature and an elevated pressure, with a particulate supported Fischer-Tropsch synthesis catalyst. The catalyst comprises a catalyst support, Co in catalytically active form supported on the catalyst support, and a dopant selected from the group consisting of platinum (Pt), palladium (Pd), ruthenium (Ru) and/or rhenium (Re). The dopant level is expressed by a formula. Hydrocarbons and, optionally, oxygenates of hydrocarbons are obtained.

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Номер записи: 14

16-08-2012 дата публикации

Selective isomerization and oligomerization of olefin feedstocks for the production of turbine and diesel fuels

Номер: US20120209046A1

Автор: Benjamin G. Harvey, Michael E Wright

Принадлежит: US Department of Navy

A process from converting alcohol feedstock to diesel/turbine fuels.

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Номер записи: 15

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: 16

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: 17

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: 18

01-11-2012 дата публикации

Process for increasing aromatics production

Номер: US20120277503A1

Автор: David A. Wegerer, Kurt M. Vanden Bussche, Mark D. Moser

Принадлежит: UOP LLC

A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated.

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Номер записи: 19

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: 20

13-12-2012 дата публикации

Methods for producing fuels and solvents substantially free of fatty acids

Номер: US20120316370A1

Автор: David Bressler

Принадлежит: University of Alberta

Described herein are methods for producing fuels and solvents from fatty acid re-extraction sources. In general, the pyrolysis products of fatty acids are extracted in order to remove residual fatty acids and produce very pure hydrocarbon compositions composed of alkanes and alkenes. The fatty acids removed from the extraction step can be further pyrolyzed to produce additional hydrocarbons or, in the alternative, the fatty acids can be isolated and used in other applications. Also disclosed herein are fuels and solvents produced by the methods described herein.

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Номер записи: 21

03-01-2013 дата публикации

Method for producing monocyclic aromatic hydrocarbons

Номер: US20130006027A1

Автор: Masahide Kobayashi, Shinichiro Yanagawa

Принадлежит: Individual

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

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Номер записи: 22

31-01-2013 дата публикации

Integrated Selective Hydrocracking and Fluid Catalytic Cracking Process

Номер: US20130026065A1

Автор: Omer Refa Koseoglu

Принадлежит: Saudi Arabian Oil Co

An integrated process and system for conversion of a heavy crude oil to produce transportation fuels is provided. The process includes separating the hydrocarbon feed into an aromatic-lean fraction and an aromatic-rich fraction. The aromatic-rich fraction is hydrocracked under relatively high pressure to convert at least a portion of refractory aromatic organosulfur and organonitrogen compounds and to produce a hydrocracked product stream. Unconverted bottoms effluent is recycled to the aromatic separation step. The aromatic-lean fraction is cracked in a fluidized catalytic cracking reaction zone to produce a cracked product stream, a light cycle oil stream and a heavy cycle oil stream. In certain embodiments the aromatic-lean fraction can be hydrotreated prior to fluidized catalytic cracking.

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Номер записи: 23

21-02-2013 дата публикации

High Output Modular CAES (HOMC)

Номер: US20130042601A1

Автор: Robert J. Kraft

Принадлежит: Robert J. Kraft

A compressed air energy storage system integrated with a source of secondary heat, such as a simple cycle gas turbine, to increase power production and to provide power regulation through the use of stored compressed air heated by said secondary heat to provide power augmentation.

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Номер записи: 24

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: 25

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: 26

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: 27

21-03-2013 дата публикации

METHOD FOR INCREASING THERMAL STABILITY OF A FUEL COMPOSITION USING A SOLID PHOSPHORIC ACID CATALYST

Номер: US20130068660A1

Автор: Bergeron Sebastien, Falkiner Robert J., Poirier Marc-André, Uppal Ashok

Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

This invention relates to a method for increasing thermal stability of fuel, as well as in reducing nitrogen content and/or enhancing color quality of the fuel. According to the method, a fuel feedstock can be treated with a solid phosphoric acid catalyst under appropriate catalyst conditions, e.g., to increase the thermal stability of the fuel feedstock. Preferably, the fuel feedstock can be treated with the solid phosphoric acid catalyst at a ratio of catalyst mass within a contact zone to a mass flow rate of feedstock through the zone of at least about 18 minutes to increase the thermal stability of the fuel feedstock, along with reducing nitrogen content and/or enhancing color quality. 1. A method for increasing thermal stability of fuel , comprising:flowing a fuel feedstock through a contact zone containing solid phosphoric acid catalyst within the contact zone, wherein the fuel feedstock has an initial and final boiling point within a range from about 90° C. to about 360° C. (194° F. to about 680° F.), and wherein the fuel feedstock is in contact with the solid phosphoric acid catalyst for a period of time of at least about 18 minutes; andproducing a fuel product that has a higher thermal stability than the fuel feedstock according to ASTM D3241-09.2. The method of claim 1 , wherein the solid phosphoric acid catalyst is comprised of silicon orthophosphate.3. The method of claim 2 , wherein the solid phosphoric acid catalyst is further comprised of silicon pyrophosphate and exhibits an integrated X-ray diffraction (XRD) reflectance peak intensity ratio of silicon orthophosphate to silicon pyrophosphate of at least about 4:1.4. The method of claim 2 , wherein the solid phosphoric acid catalyst has a silicon phosphate crystallinity of at least 25% relative to an alpha-alumina standard.5. The method of claim 1 , wherein the solid phosphoric acid catalyst is comprised of pyrophosphate crystallites with at least 0.1% crystallinity (as measured by X-ray diffraction) ...

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Номер записи: 28

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: 29

21-03-2013 дата публикации

PROCESS AND APPARATUS FOR PRODUCING HYDROCARBONS FROM FEED-STOCKS COMPRISING TALL OIL AND TERPENE-COMPOUNDS

Номер: US20130072730A1

Автор: KNUUTTILA Pekka, NOUSIAINEN Jaakko, RISSANEN Arto

Принадлежит: UPM-KYMMENE CORPORATION

The invention relates to a process for producing hydrocarbon components, comprising: providing a feedstock comprising tall oil and terpene-based compounds; subjecting the feedstock and a hydrogen gas feed to a hydroprocessing treatment in the presence of a hydroprocessing catalyst to produce hydrocarbon components including n-paraffins, and subjecting the hydrocarbon components including n-paraffins to isomerisation in the presence of a dewaxing catalyst to form a mixture of hydrocarbon components. The invention also relates to an apparatus for implementing the process. The invention further relates to a use of the hydrocarbon components produced by the process as a fuel or as an additive in fuel compositions. The invention also relates to a use of a NiW catalyst on a support selected from AlO, zeolite, zeolite-AlO, and AlO—SiOfor producing fuel or an additive for fuel compositions from a feedstock comprising tall oil and terpene-based compounds. 123-. (canceled)24. A process for producing hydrocarbon components , comprising:providing a feedstock comprising tall oil and terpene-based compounds;{'sub': 3', '2', '3, 'subjecting the feedstock and a hydrogen gas feed to a hydroprocessing treatment in the presence of a NiO/MoOcatalyst on an AlOsupport to produce hydrocarbon components including n-paraffins, and'}{'sub': 2', '3, 'subjecting the hydrocarbon components including n-paraffins to isomerisation in the presence of a NiW catalyst on a zeolite-AlOsupport and in the presence of hydrogen to form a mixture of hydrocarbon components.'}25. The process according to wherein the terpene-based compounds are obtained from plants claim 24 , terpene oils claim 24 , distillation bottoms from terpene distillation and flavorants and/or fragrance industry.26. The process of wherein the feedstock comprises crude tall oil and crude sulphate turpentine derived from kraft pulping of wood.27. The process of wherein the crude tall oil is purified prior to subjecting it to the ...

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Номер записи: 30

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: 31

28-03-2013 дата публикации

Process For The Hydrogenation Of Fatty Acids Using A Promoted Supported Nickel Catalyst

Номер: US20130079535A1

Автор: Robert Johan Andreas Maria Terorde, Tjalling Rekker

Принадлежит: BASF Corp

The invention is directed to a process for the hydrogenation of unsaturated fatty acids to produce saturated fatty acids, said process comprising hydrogenating the unsaturated fatty acid in the presence of hydrogen and a supported nickel catalyst, said supported nickel catalyst comprising an oxidic support, 5 to 80 wt. % of nickel, calculated as metallic nickel on the weight of the catalyst, and 0.1 to 10 wt. % of a manganese promoter, calculated as MnO 2 on the weight of the catalyst.

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Номер записи: 32

04-04-2013 дата публикации

Method for the hydroconversion of oil feedstocks using slurry technology, allowing the recovery of metals from the catalyst and the feedstock, comprising an extraction step

Номер: US20130081976A1

Автор: Alain Quignard, Frederic Morel, Jean-Philippe Heraud

Принадлежит: IFP Energies Nouvelles IFPEN

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, at least one liquid/liquid extraction step, a combustion step, a metals extraction step and a step for the preparation of catalytic solutions which are recycled to the hydroconversion step.

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Номер записи: 33

04-04-2013 дата публикации

USE OF LOW BOILING POINT AROMATIC SOLVENT IN HYDROPROCESSING HEAVY HYDROCARBONS

Номер: US20130081978A1

Автор: Brown Stephen Harold, Cheng Jane Chi-ya, Ho Teh C., Woo Hyung Suk

Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

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

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Номер записи: 34

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: 35

11-04-2013 дата публикации

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

Номер: US20130087482A1

Автор: Laura E. Leonard, Robert Haizmann

Принадлежит: UOP LLC

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

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Номер записи: 36

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: 37

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: 38

02-05-2013 дата публикации

METHOD FOR PREPARING LUBRICATING BASE OILS BY USING VACUUM DISTILLED DEASPHALTED OIL

Номер: US20130105359A1

Автор: Choi Sun, Chun Bum Suk, Kim Do Hyoun, Kim Do Woan, Kim Gyung Rok, LEE Seung Woo, Noh Kyung Seok, Oh Seung Hoon, Ryu Jae Wook, Yoon Byung Won

Принадлежит: SK INNOVATION CO., LTD.

The present invention relates to a method for preparing lubricating base oils by using vacuum distilled deasphalted oil, and more specifically, to a method for preparing various kinds of lubricating base oils by distilling a distillate obtained from a solvent deasphalting (SDA) process under reduced pressure to obtain heavy deasphalted oil (H-DAO) and light deasphalted (Lt-DAO) and then treating the H-DAO and the Lt-DAO by catalytic reactions, respectively. According to the present invention, it is possible to obtain heavy lubricating base oil (150BS) of a high viscosity grade which can not be obtained by a known catalytic reaction and a lubricating base oil of group III by hydrogenation, in a high yield, and thus economical efficiency is excellent. 1. A method of producing heavy lubricating base oil using vacuum-distilled deasphalted oil , comprising the steps of:(a) introducing atmospheric residual oil or a mixture of atmospheric residual of and vacuum residual oil into a solvent deasphalting apparatus to obtain deasphalted oil;(b) vacuum-distilling the deasphalted oil to obtain light deasphalted oil and heavy deasphalted oil;(c) hydrotreating the heavy deasphalted oil obtained in the step (b) in the presence of a hydrogenation catalyst to obtain a hydrotreated fraction;(d) dewaxing the hydrotreated fraction obtained in the step (c) in the presence of a dewaxing catalyst; and(e) hydrofinishing the dewaxed fraction obtained in the step (d) in the presence of a hydrofinishing catalyst.2. The method of claim 1 , further comprising the step: (f) fractionating the hydrofinished fraction obtained in the step (e) according to a viscosity range to obtain heavy lubricating base oil.3. The method of claim 1 , wherein claim 1 , in the step (c) claim 1 , the hydrotreating of the heavy deasphalted oil is performed under the conditions of a reaction temperature of 300 to 410° C. claim 1 , a reaction pressure of 30 to 220 kg/cmg and a liquid hourly space velocity (LHSV) of 0.1 ...

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Номер записи: 39

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: 40

02-05-2013 дата публикации

Fuel compositions containing an isomerized component of a single carbon number and methods of preparing the fuel compositions

Номер: US20130109893A1

Автор: Heinz J. Robota, Jhoanna C. Alger

Принадлежит: University of Dayton

Fuel compositions containing an isomerized component of a single carbon number may contain at least 97 wt. %, based on the total weight of the fuel composition, of an isomerized component consisting of aliphatic paraffin isomers all having the formula C n H 2n+2 , where 10≦n≦22 and n has the same value for each aliphatic paraffin isomer in the isomerized component. The fuel compositions have a normal alkane content of less than 10 wt. %, based on the total weight of the fuel composition. Methods for preparing the fuel compositions include hydroisomerizing a normal alkane starting material to form an isomerized mixture and subsequently removing remnant normal alkanes from the isomerized mixture by solvent dewaxing and/or distillation. Some of the fuel compositions may have freezing points at or below −47° C., making them amenable for use a surrogate fuels in the place of JP-8.

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Номер записи: 41

09-05-2013 дата публикации

Process for the conversion of heavy charge stocks such as heavy crude oils and distillation residues

Номер: US20130112593A1

Автор: Alberto Delbianco, Mario Marchionna, Nicoletta Panariti, Romolo Montanari, Sergio Rosi

Принадлежит: Eni Spa

Process for the conversion of heavy charge stocks selected from heavy and extra-heavy crude oils, distillation residues, heavy oils from catalytic treatment, thermal tars, bitumens from oil sands, carbons of different origins and other high boiling charges of a hydrocarbon origin known as “black oils”, using at least the following process units: solvent deasphalting (SDA), hydroconversion with slurry phase catalysts (HT), distillation or flash (D), which process includes: solvent deasphalting, thereby forming a deasphthalted oil (DAO), as described; hydrotreating the DAO in the presence of a hydrogenation catalyst precursor and hydrogen or hydrogen and H 2 S, as described; sending the product therefrom to distillation or flash (D) step(s), and separating the most volatile fractions from the distillation residue (tar) or from the liquid coming from the flash unit, as described; recycling at least a portion of the tar or the liquid, to the hydrotreating section, as described.

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Номер записи: 42

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: 43

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: 44

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: 45

09-05-2013 дата публикации

FUEL COMPOSITION

Номер: US20130116487A1

Автор: Clark Alisdair Quentin, Howard Philip, Parker Anthony George

Принадлежит: BP Oil International Limited

Unleaded blend composition having a Motor Octane Number (MON) of at least 80 having less than 42% of aromatic compounds, and at least 2% by volume of the total composition of component (a′), which is a substantially aliphatic hydrocarbon refinery stream of MON value of at least 85. At least 70% in total of the stream is branched chain alkanes, the stream being obtained by distillation from a refinery material as a cut having Initial Boiling Point of at least 15° C. and Final Boiling Point of at most 160° C. The Boiling Points are measured according to ASTMID2892. At least 5% of at least one paraffin, aromatic hydrocarbon compound or olefinic hydrocarbon has a bp 60-160° C., with not more than 5% of the total composition of hydrocarbon having a bp more than 160° C. Less than 5% 2,2,3-trimethylbutane or 2,2,3-trimethylpentane is present. 1142-. (canceled)143. An unleaded blend composition having a Motor Octane Number (MON) of at least 80 comprising less than 42% of aromatic compounds , and at least 2% (by volume of the total composition) of component (a′) , which is a substantially aliphatic hydrocarbon refinery stream of MON value of at least 85 , at least 70% in total of said stream being branched chain alkanes , said stream being obtained by distillation from a refinery material as a-cut having Initial Boiling Point of at least 15° C. and Final Boiling Point of at most 160° C. , said Boiling Points being measured according to ASTMID2892 , and at least 5% of at least one paraffin , aromatic hydrocarbon compound or olefinic hydrocarbon of b.p. 60-160° C. , with not more than 5% of the total composition of hydrocarbon of bp more than 160° C. , and less than 5% 2 ,2 ,3-trimethylbutane or 2 ,2 ,3-trimethylpentane.144. An unleaded blend composition having a Motor Octane Number (MON) of at least 80 comprising less than 42% of aromatic compounds at least 5% (by volume of the total composition) of component (a′) , which is at least one branched chain alkane of MON value of ...

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Номер записи: 46

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: 47

23-05-2013 дата публикации

DIESEL ENGINE INJECTOR FOULING IMPROVEMENTS WITH A HIGHLY PARAFFINIC DISTILLATE FUEL

Номер: US20130125849A1

Автор: Schaberg Paul Werner, Velaers Adrian James

Принадлежит: SASOL TECHNOLOGY (PTY) LTD.

The invention provides the use of a highly paraffinic distillate fuel in a diesel fuel composition for reducing the formation of injector nozzle deposits when combusted in a diesel engine having a high pressure fuel injection system, wherein the distillate fuel has an aromatics content less than 0.1 wt %, a sulphur content less than 10 ppm and a paraffinic content of at least 70 wt %, such that the diesel fuel composition has a relative fouling behaviour of 70% or less and a density of more than 0.815 g.cm(at 15° C.). 1. A highly paraffinic distillate fuel for use in a diesel fuel composition for reducing the formation of injector nozzle deposits when combusted in a diesel engine having a high pressure fuel injection system , wherein the highly paraffinic distillate fuel has an aromatics content less than 0.1 wt % , a sulphur content less than 10 ppm and a paraffinic content of at least 70 wt % , such that the diesel fuel composition has a relative fouling behaviour of 70% or less and a density of more than 0.815 g.cm(at 15° C.).2. The highly paraffinic distillate fuel of claim 1 , wherein the diesel fuel composition has a relative fouling behaviour of 60% or less.3. The highly paraffinic distillate fuel of claim 1 , wherein the diesel fuel composition has a relative fouling behaviour of 50% or less and a density of more than 0.79 g.cm(at 15° C.).4. The highly paraffinic distillate fuel of claim 1 , wherein the highly paraffinic distillate fuel is derived from a Fischer Tropsch process claim 1 , a hydrogenated renewable oil claim 1 , or a combination thereof.5. The highly paraffinic distillate fuel of claim 1 , wherein the highly paraffinic distillate fuel has a cetane number greater than 70.6. The highly paraffinic distillate fuel of claim 1 , wherein the diesel fuel composition comprises a petroleum-derived distillate fuel claim 1 , a bio-derived fuel claim 1 , or a combination thereof.7. The highly paraffinic distillate fuel of claim 1 , wherein the diesel fuel ...

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Номер записи: 48

23-05-2013 дата публикации

CATALYTIC HYDROGENATION OF HYDROXYCYCLOALKANES AND USE OF THE PRODUCT IN BIOFUEL COMPOSITIONS FOR AVIATION

Номер: US20130131407A1

Автор: Dos Reis Goncalves Flavio, Fraga Marco Andre, Pizzaro Borges Luis Eduardo

Принадлежит:

This invention relates to a new biofuel alternative to be used in aviation sector, starting from obtention and production routes of renewable sources compounds, that may act as load for aviation kerosene composition. Naphthenic compounds (cycloalkanes) obtained from renewable sources are used as enrichment or addition loads of aviation kerosene. The process is based on hydrogenolysis catalytic reactions, from hydroxycycloalkanes derevatives substrata, like menthol and isopulegol. The catalytic system is constituted of a physical mixture of hydrogenation heterogeneous catalysts, acid heterogeneous catalysts, and hydrogenating metallic catalysts in acid supports. The hydrogenation catalysts used envolve noble metals from groups 6, 7, 8, 9 and 10 of periodic table, whose content ranges from 0.01-10%. The heterogeneous catalysts suitable acids are represented by acidic sulfonated polymer resins, protonated zeolites and sulfated zirconia. The catalytic reaction conditions involving a temperature range of 70-250° C., pressure between 1-70 and agitation ranging from 100-1000 rpm. The composition involving the biofuel, obtained by catalytic hydrogenation process, is obtained as a mixture composed by cycloalkanes and aviation fuel in ratio 1:100 to 100:1, in volume. 1. A biomass hydrogenolysis catalytic process comprising:a catalytic hydrogenation reaction of hydroxycycloalkanes derivatives to obtain biofuel for aviation, biokerosene composed mainly by cycloalkanes.2. The process according to claim 1 , wherein the catalytic system includes mixtures of hydrogenation heterogeneous catalysts and acid heterogeneous catalysts claim 1 , or bifunctional catalysts constituted of acid support and active phase by hydrogenating metal.3. The process according to claim 2 , wherein the mass ratio of hydrogenation heterogeneous catalyst:acid heterogeneous catalyst comprises 5:1 to 1:5 range claim 2 , more preferably the range between 2:1 and 1:2.4. The process according to claim 2 , ...

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Номер записи: 49

23-05-2013 дата публикации

EVEN CARBON NUMBER PARAFFIN COMPOSITION AND METHOD OF MANUFACTURING SAME

Номер: US20130131408A1

Автор: Abhari Ramin, Gruver Vladimir, Tomlinson H. Lynn

Принадлежит: Syntroleum Corporation

Paraffin compositions including mainly even carbon number paraffins, and a method for manufacturing the same, is disclosed herein. In one embodiment, the method involves contacting naturally occurring fatty acid/glycerides with hydrogen in a slurry bubble column reactor containing bimetallic catalysts with equivalent particle diameters from about 10 to about 400 micron. The even carbon number compositions are particularly useful as phase change material. 1. A composition comprising C-Cparaffins , wherein:the paraffins are produced from a renewable biological feedstock by a process comprising hydrogenation and hydrogenolysis; andthe paraffins are predominately even carbon number paraffins.2. The composition of claim 1 , wherein the even carbon number paraffins comprise n-hexadecane and n-octadecane.3. The composition of claim 1 , wherein the even carbon number paraffins comprise n-dodecane and n-tetradecane.4. The composition of claim 1 , wherein at least 75 wt % of the paraffins are even carbon number paraffins.5. The composition of claim 1 , wherein at least 80 wt % of the paraffins are even carbon number paraffins.6. The composition of claim 1 , wherein the renewable biological feedstock is selected from the group consisting of vegetable oils claim 1 , plant oils claim 1 , algal oils claim 1 , animal fats claim 1 , tall oil fatty acid claim 1 , products of the food industry claim 1 , and a combination of any two or more thereof.7. The composition of claim 1 , wherein the renewable biological feedstock is selected from the groups consisting of soybean oil claim 1 , corn oil claim 1 , cottonseed oil claim 1 , canola oil claim 1 , coconut oil claim 1 , sunflower oil claim 1 , palm oil claim 1 , palm kernel oil claim 1 , rapeseed oil claim 1 , and a combination of any two or more thereof.8. The composition of claim 1 , wherein the renewable biological feedstock is selected from the group consisting of soybean oil claim 1 , canola oil claim 1 , palm oil claim 1 , palm ...

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Номер записи: 50

30-05-2013 дата публикации

FLUIDIZED CATALYTIC CRACKING OF PARAFFINIC NAPHTHA IN A DOWNFLOW REACTOR

Номер: US20130137909A1

Автор: DEAN Christopher F., FOX Allan Birkett, LONGSTAFF Daniel C.

Принадлежит:

A process for producing a product stream consisting primarily of the lower olefins ethylene, propylene and butylenes, and of gasoline is provided. The process includes cracking a mixture of paraffinic naphtha feedstream and regenerated catalyst in a downflow reactor. The reaction product stream is separated from the spent catalyst and subsequently fractionated into individual product streams, while the spent catalyst is regenerated and recycled. 1. A method of enhancing the conversion of a major proportion of a paraffinic naphtha feedstream into lighter hydrocarbon reaction products that include a high proportion of the lower olefins ethylene , propylene and butylenes , and gasoline , the method comprising:a. introducing a feedstream containing a minimum of 40% by weight of paraffinic naphtha boiling in the range of from 30° C. (86° F.) to 200° C. (392° F.), or a feedstream containing a minimum of 60% by weight of combined paraffinic naphtha and naphthenic compounds into the top of a downflow reactor and mixing it with catalyst;b. operating the downflow reactor with a residence time of 0.1 seconds to 5 seconds of the mixture of the feedstream and catalyst in a reaction zone at an operating temperature in the range of 480° C. (896° F.) to 700° C. (1292° F.) and with a catalyst-to-feedstream ratio in the range of from 25:1 to 80:1 by weight to produce a reaction product stream that includes the lower olefins ethylene, propylene and butylenes, and gasoline;c. separating the reaction product stream produced in the downflow reactor from spent catalyst in a stripper zone downstream of the reaction zone;d. recovering the reaction product stream from the stripper zone;e. passing spent catalyst from the stripper zone to a dedicated regeneration vessel for regeneration with a supplemental source of heat to increase the temperature in the regeneration vessel, the regeneration vessel receiving spent catalyst only from the downflow reactor and, optionally, other reactors in ...

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Номер записи: 51

06-06-2013 дата публикации

RENEWABLE JET FUEL DERIVED FROM BIOMASS

Номер: US20130144090A1

Автор: Brown Ronald E., Dunn Brian C., Fjare Kristi A., Gerritsen Leendert Arie, Lotero Edgar, Marshall Stephen, Pansare Sourabh S., Platon Alexandru

Принадлежит: Phillips 66 Company

A single pass direct conversion of biomass derived oxygenates to longer chain hydrocarbons is described. The longer chain hydrocarbons include higher naphthene content which is quite useful in the distillate range fuels or more particularly, the jet and diesel range fuels. Naphthenes help the biomass derived hydrocarbons meet product specifications for jet and diesel while really helping cold flow properties. 1. A renewable jet fuel derived at least in part from biomass comprising:approximately 0 to 10 wt % n-paraffins,approximately 5 to 20 wt % iso-paraffins,approximately 15% to 95 wt % naphthenes,approximately 5 to 50 wt % 1-ring naphthenes,approximately 0 to 50 wt % 2-ring naphthenes,approximately 0 to 10 wt % 3-ring naphthenes, andapproximately 0 to 25 wt % aromatics.2. A renewable jet fuel according to comprising at least 25 weight percent naphthenes.3. A renewable jet fuel according to comprising at least 45 weight percent naphthenes.4. A renewable jet fuel according to comprising at least 70 weight percent naphthenes.5. A renewable jet fuel according to comprising up to a maximum of 90 weight percent naphthenes.6. The renewable jet fuel according to having a freeze point of less than −40 degrees Fahrenheit.7. The renewable jet fuel according to having a flashpoint greater than 100 degrees Fahrenheit.8. The renewable jet fuel according to wherein at least 95% of the jet fuel is derived from biomass.9. The renewable jet fuel according to wherein at least 90% of the jet fuel is derived from biomass.10. The renewable jet fuel according to wherein the jet fuel is a drop in jet fuel that meets all specifications for Jet A and JP-8. This application is a non-provisional application which claims benefit under 35 USC §119(e) to U.S. Provisional Application Ser. No. 61/567,287 filed Dec. 6, 2011, entitled “Direct Conversion of Biomass Oxygenates to Distillate-Range Hydrocarbons,” which is incorporated herein in its entirety. This application is also a non-provisional ...

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Номер записи: 52

06-06-2013 дата публикации

RENEWABLE DIESEL FUEL DERIVED FROM BIOMASS

Номер: US20130144091A1

Автор: Brown Ronald E., Dunn Brian C., Fjare Kristi A., Gerritsen Leendert Arie, Lotero Edgar, Marshall Stephen, Pansare Sourabh S., Platon Alexandru

Принадлежит: Phillips 66 Company

A single pass direct conversion of biomass derived oxygenates to longer chain hydrocarbons is described. The longer chain hydrocarbons include higher naphthene content which is quite useful in the distillate range fuels or more particularly, the jet and diesel range fuels. Naphthenes help the biomass derived hydrocarbons meet product specifications for jet and diesel while really helping cold flow properties. 1. A renewable diesel fuel derived at least in part from biomass comprising:approximately 0 to 10 wt % n-paraffins,approximately 5 to 20 wt % iso-paraffins,approximately 15% to 95 wt % naphthenes,approximately 5 to 50 wt % 1-ring naphthenes,approximately 5 to 50 wt % 2-ring naphthenes,approximately 0 to 15 wt % 3-ring naphthenes, andapproximately 0 to 25 wt % aromatics.2. A renewable diesel fuel according to comprising at least 25 weight percent naphthenes.3. A renewable diesel fuel according to comprising at least 45 weight percent naphthenes.4. A renewable diesel fuel according to comprising at least 70 weight percent naphthenes.5. A renewable diesel fuel according to comprising up to a maximum of 92 weight percent naphthenes.6. The renewable diesel fuel according to having a cloud point of less than −20 degrees Fahrenheit and a pour point of less than −20 degrees Fahrenheit.7. The renewable diesel fuel according to having a flashpoint greater than 125 degrees F.8. The renewable diesel fuel according to having a cetane rating of at least 40.9. The renewable diesel fuel according to wherein at least 95% of the diesel fuel is derived from biomass.10. The renewable diesel fuel according to wherein at least 90% of the diesel fuel is derived from biomass.11. The renewable diesel fuel according to wherein the jet fuel is a drop in diesel fuel that meets all specifications for Number 2 Diesel. This application is a non-provisional application which claims benefit under 35 USC §119(e) to U.S. Provisional Application Ser. No. 61/567,287 filed Dec. 6, 2011, entitled “ ...

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Номер записи: 53

06-06-2013 дата публикации

Renewable gas oil derived from biomass

Номер: US20130144094A1

Автор: Alexandru Platon, Brian C. Dunn, Edgar LOTERO, Kristi A. Fjare, Leendert Arie Gerritsen, Ronald E. Brown, Sourabh S. Pansare, Stephen Marshall

Принадлежит: Phillips 66 Co

A single pass direct conversion of biomass derived oxygenates to longer chain hydrocarbons is described. The longer chain hydrocarbons include higher naphthene content which is quite useful in the distillate range fuels or more particularly, the jet and diesel range fuels. Naphthenes help the biomass derived hydrocarbons meet product specifications for jet and diesel while really helping cold flow properties.

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Номер записи: 54

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: 55

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: 56

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: 57

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: 58

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: 59

27-06-2013 дата публикации

HYDROPROCESSING OF HEAVY HYDROCARBON FEEDS

Номер: US20130161237A1

Автор: Barrai Federico, Brown Stephen Harold, Cheng Jane Chi-ya, Dougherty Richard Charles, Ferrughelli David Thomas, Ho Teh C., Woo Hyung Suk

Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Heavy oil feeds are hydroprocessed in the presence of a solvent under conditions that provide a variety of benefits. The solvent can be an added solvent or a portion of the liquid effluent from hydroprocessing. The processes allow for lower pressure processing of heavy oil feeds for extended processing times or extended catalyst lifetimes be reducing or mitigating the amount of coke formation on the hydroprocessing catalyst. 1. A process for producing a hydroprocessed product , comprising:{'sup': '−1', 'exposing a combined feedstock comprising a heavy oil feed component and a solvent component to a hydroprocessing catalyst under effective hydroprocessing conditions to form a hydroprocessed effluent, the effective hydroprocessing conditions including a partial pressure of hydrogen of about 1000 psia (6.9 MPa) or less, a temperature of at least about 360° C., and a liquid hourly space velocity of the fraction of the combined feedstock boiling above 1050° F. (5660) of at least about 0.10 hr;'}separating the hydroprocessing effluent to form at least a liquid effluent; andfractionating a first portion of the liquid effluent to form at least a distillate product and a bottoms product, the bottoms product having an ASTM D86 distillation point of at least about 600° F. (316° C.).2. The process of claim 1 , wherein the 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 process 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 process of claim 1 , wherein the effective hydroprocessing conditions comprise a partial pressure of hydrogen of about 800 psia (5.5 MPa) or less.5. The process of claim 1 , wherein the effective hydroprocessing conditions comprise a total pressure of about 1000 psig (6.9 MPag) or less.6. The process of claim 1 , wherein the liquid hourly ...

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Номер записи: 60

27-06-2013 дата публикации

PROCESS FOR INCREASED PRODUCTION OF FCC GASOLINE

Номер: US20130165717A1

Автор: DAAGE Michel, Dandekar Ajit Bhaskar, Johnson David Lee, Liou Jiunn-Shyan, Lowenthal Steven S., McCarthy Stephen John, VIJAY Rohit

Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

This invention relates to methods and processes for increasing the production of FCC (Fluid Catalytic Cracking) gasoline products, and optionally distillate products, from refinery feedstocks. In particular, the processes include hydrotreating and further hydroisomerizing a typical FCC range feedstream prior to catalytically cracking the feedstream in the FCC unit. The methods herein result in higher FCC naphtha yields and lower FCC cat bottoms yields thereby significantly increasing the overall FCC gasoline production for a given operating unit and increasing the profit margin of such FCC unit operations. 1. A process for increasing Fluid Catalytic Cracking (“FCC”) gasoline production comprising:a) contacting a hydrocarbon-containing hydroisomerization feedstream with a hydroisomerization catalyst under hydroisomerization conditions to produce at least one hydroisomerized liquid product stream that has a higher iso-paraffin content than the hydroisomerization feedstream;b) contacting in the reaction zone of an FCC reactor riser an FCC feedstream comprising at least a portion of the hydroisomerized liquid product stream of step a) with a fluid catalytic cracking catalyst thereby catalytically cracking the FCC feedstream into an FCC product that has an average lower boiling point than the FCC feedstream, and producing a spent catalyst;c) the FCC product from the spent catalyst;d) cooling the FCC product; ande) fractionating the FCC product into multiple FCC product streams, wherein at least one of the FCC product streams is a naphtha boiling-range product stream; andf) utilizing at least a portion of the naphtha boiling-range product stream for gasoline production.2. The process of claim 1 , wherein at least 50 wt % of the normal paraffins in the hydroisomerization feedstream are converted to iso-paraffins in the hydroisomerized liquid product stream in step a).3. The process of claim 2 , wherein the hydroisomerization catalyst comprises at least one Group VIIIA ...

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Номер записи: 61

04-07-2013 дата публикации

Spherical Magnet

Номер: US20130169396A1

Автор: Michael Miller

Принадлежит: Individual

A spherical magnet is formed as a hollow sphere having a fluid tight outer surface of a first magnetic pole and an inner surface having a second magnetic pole that is magnetically opposite the first pole. A plurality of individual thin flexible rectangular plate magnets are arranged as a continuous outer layer of the spherical magnet. Each individual plate magnet has four sides, an inner magnetic portion and an outer non-magnetic portion that extends around all four sides of the magnetic portion. Each inner magnetic portion includes a first face disposed on the outer surface and having the first pole and a second face opposite the first face, disposed on the inner surface and having the second pole.

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Номер записи: 62

11-07-2013 дата публикации

Thermal Energy Conversion System

Номер: US20130174554A1

Автор: Brewer Michael Anthony

Принадлежит: GRAVATON ENERGY RESOURCES LTD, LLC

A power generation system includes a first vessel having a generally constant volume and a second vessel having a variable volume. Thermal energy is supplied to an ideal gas within the first vessel in order to raise its temperature and pressure. The thermally compressed gas is then released into, and expands the volume of, the second vessel. The expanding volume of the second vessel expands raises a mass and/or strains an elastic member, thus storing gravitational and/or elastic potential energy. This stored potential energy can be released on demand by evacuating the second vessel, typically into a third vessel, and used to power a generator. Preferably, the potential energy is used to coupled to the generator using a planetary gear drive, such that a relatively small number of input rotations yields a relatively large number of output rotations. 1. A power generation system , comprising:at least one thermal energy accumulation vessel containing a gas;a potential energy generation system, including at least one battery vessel connected to the at least one thermal energy accumulation vessel and having a variable volume,wherein the potential energy generation system generates and stores potential energy via expansion of the volume of the at least one battery vessel when a quantity of the gas moves from the at least one thermal energy accumulation vessel to the at least one battery vessel after increasing in temperature while in the at least one thermal energy accumulation vessel;a thermal energy dissipation vessel connected to the at least one battery vessel; andan energy conversion system coupled to the potential energy generation system,wherein the energy conversion system converts potential energy stored by the potential energy generation system into electrical energy when a quantity of the gas is evacuated from the at least one battery vessel to the thermal energy dissipation vessel after expansion of the volume of the at least one battery vessel.2. The power ...

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Номер записи: 63

18-07-2013 дата публикации

Hydrocarbon feedstock average molecular weight increase

Номер: US20130180884A1

Автор: Cyril Revault, Delphine Minoux

Принадлежит: Total Raffinage Marketing SA

The invention deals with hydrocarbon feedstock molecular weight increase via olefin oligomerization and/or olefin alkylation onto aromatic rings. Addition of a purification section allows improved unit working time and lower maintenance.

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Номер записи: 64

18-07-2013 дата публикации

Method for reducing coke deposition

Номер: US20130184510A1

Автор: HE Huang, Martin Haas

Принадлежит: United Technologies Corp

A method for reducing coke deposits includes heating an alcohol-fuel mixture to decompose alcohol and form water to produce a fuel-water mixture and delivering the fuel-water mixture to a carbon-steam gasification catalyst. The fuel-water mixture reacts with the carbon-steam gasification catalyst such that coke deposits are prevented from remaining in a space near the carbon-steam gasification catalyst.

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Номер записи: 65

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: 66

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: 67

01-08-2013 дата публикации

INTEGRATED HYDROTREATING AND STEAM PYROLYSIS PROCESS INCLUDING RESIDUAL BYPASS FOR DIRECT PROCESSING OF A CRUDE OIL

Номер: US20130197283A1

Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

A process is provided that is directed to a steam pyrolysis zone integrated with a hydroprocessing zone including residual bypass to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. The integrated hydrotreating and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals comprises separating the crude oil into light components and heavy components; charging the light components and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity; thermally cracking the hydroprocessed effluent in the presence of steam to produce a mixed product stream; separating the mixed product stream; purifying hydrogen recovered from the mixed product stream and recycling it to the hydroprocessing zone ; recovering olefins and aromatics from the separated mixed product stream; and recovering a combined stream of pyrolysis fuel oil from the separated mixed product stream and heavy components from step (a) as a fuel oil blend. 1. An integrated hydrotreating and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals , the process comprising:a. separating the crude oil into light components and heavy components;b. charging the light components and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity;c. thermally cracking the hydroprocessed effluent in the presence of steam to produce a mixed product stream;d. separating the thermally cracked mixed product stream;e. ...

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Номер записи: 68

01-08-2013 дата публикации

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

Номер: US20130197284A1

Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, SAYED Essam, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

A process is provided that is directed to a steam pyrolysis zone integrated with a hydrotreating zone and a solvent deasphalting zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. The integrated hydrotreating, solvent deasphalting and steam pyrolysis process comprises charging the crude oil to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity; charging the hydroprocessed effluent to a solvent deasphalting zone with an effective amount of solvent to produce a deasphalted and demetalized oil stream and a bottom asphalt phase; thermally cracking the deasphalted and demetalized oil stream in the presence of steam to produce a mixed product stream; separating the mixed product stream; purifying hydrogen recovered from the mixed product stream and recycling it to the hydroprocessing zone; recovering olefins and aromatics from the separated mixed product stream; and recovering pyrolysis fuel oil from the separated mixed product stream. 1. An integrated hydrotreating , solvent deasphalting and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals , the process comprising:a. charging the crude oil to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity;b. charging the hydroprocessed effluent to a solvent deasphalting zone with an effective amount of solvent to produce a deasphalted and demetalized oil stream and a bottom asphalt phase;c. thermally cracking the deasphalted and demetalized oil stream in the presence of ...

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Номер записи: 69

01-08-2013 дата публикации

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

Номер: US20130197285A1

Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, HASSELMEYER Julio, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

An integrated hydrotreating and steam pyrolysis process for the direct processing of a crude oil is provided to produce olefinic and aromatic petrochemicals. Crude oil and hydrogen are charged to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity. Hydroprocessed effluent is thermally cracked in the presence of steam to produce a mixed product stream, which is separated. Hydrogen from the mixed product stream is purified and recycled to the hydroprocessing zone, and olefins and aromatics are recovered from the separated mixed product stream. 1. An integrated hydrotreating and steam pyrolysis process for the direct processing of crude oil to produce olefinic and aromatic petrochemicals , the process comprising:a. charging the crude oil and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity;b. thermally cracking hydroprocessed effluent in the presence of steam in a steam pyrolysis zone to produce a mixed product stream;c. separating the thermally cracked mixed product stream into hydrogen, olefins, aromatics and pyrolysis fuel oil;d. purifying hydrogen recovered in step (c) and recycling it to step (a);e. recovering olefins and aromatics from the separated mixed product stream; andf. recovering pyrolysis fuel oil from the separated mixed product stream.2. The integrated process of claim 1 , further comprising separating the hydroprocessed effluent from the hydroprocessing zone into a heavy fraction and a light fraction in a hydroprocessed effluent separation zone claim 1 , wherein the light fraction is the hydroprocessed effluent ...

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Номер записи: 70

08-08-2013 дата публикации

RANKINE CYCLE SYSTEM AND METHOD

Номер: US20130199173A1

Автор: Baker, Hoehne Mark R., JR. George A., Mross Greg, Voss Mark G.

Принадлежит: MODINE MANUFACTURING COMPANY

A Rankine cycle system and method is described and illustrated, and in some embodiments includes an expander, a pump, a condenser, and a receiver comprising a variable fluid volume at least partially defined by a movable member, wherein the variable fluid volume defines at least a portion of the working fluid flow path between the condenser and the inlet of the pump. Also, a method of charging a Rankine cycle system with working fluid is described and illustrated, and can include applying a regulated pressure to a chamber located within a receiver, introducing the working fluid to the Rankine cycle system, the working fluid being separated from the chamber by a movable member of the receiver, monitoring displacement of the movable member, and stopping the introduction of working fluid into the Rankine cycle system when the movable member reaches a predetermined position. 1. A Rankine cycle system comprising:an expander;a pump;a condenser located along a working fluid flow path between an outlet of the expander and an inlet of the pump; anda receiver comprising a variable fluid volume at least partially defined by a movable member, wherein the variable fluid volume defines at least a portion of the working fluid flow path between the condenser and the inlet of the pump.2. The system of claim 1 , further comprising a liquid sub-cooler located along the working fluid flow path between the receiver and the inlet of the pump.3. The system of claim 2 , wherein the condenser and the liquid sub-cooler are parts of a single heat exchanger.4. The system of claim 1 , wherein at least a portion of the variable fluid volume defines a cylindrical volume claim 1 , the movable member defining an end of the cylindrical volume.5. The system of claim 4 , wherein the movable member is movably disposed within the receiver so as to vary the length of the cylindrical volume.6. The system of claim 1 , wherein the variable fluid volume is a first variable fluid volume claim 1 , the receiver ...

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Номер записи: 71

08-08-2013 дата публикации

MILD HYDRODESULFURIZATION INTEGRATING GAS PHASE CATALYTIC OXIDATION TO PRODUCE FUELS HAVING AN ULTRA-LOW LEVEL OF ORGANOSULFUR COMPOUNDS

Номер: US20130199968A1

Автор: BOURANE Abdennour, Ismagilov Zinfer, Kerzhentsev Mikhail, KOSEOGLU Omer Refa, Parmon Valentin, Yashnik Svetlana

Принадлежит:

Desulfurization of hydrocarbon feeds is achieved by first contacting the entire feed with a hydrodesulfurization catalyst in a hydrodesulfurization reaction zone operating under mild conditions; a flashing column downstream of the hydrodesulfurization reaction zone fractionates the effluent to obtain a first fraction which contains refractory organosulfur compounds and a second fraction that is substantially free of organosulfur compounds, since the organosulfur compounds boiling in the range of this fraction were the labile organosulfur compounds which were initially removed by mild hydrodesulfurization. The first fraction is contacted with a gaseous oxidizing agent over an oxidation catalyst having a formula CuZnAlOin a gas phase catalytic oxidation reaction zone to convert the refractory organosulfur compounds to SOand low sulfur hydrocarbons. The by-product SOis subsequently removed, producing a stream containing a reduced level of organosulfur compounds. 1. A method of processing a hydrocarbon feed to remove undesired organosulfur compounds comprising:a. subjecting the hydrocarbon feed to a hydrodesulfurizing process to produce a hydrotreated effluent;b. flashing the hydrotreated effluent to provide a low boiling temperature fraction that contains a reduced level of organosulfur compounds and a high boiling temperature fraction having refractory organosulfur compounds;c. separating the high and low boiling temperature fractions; and{'sub': x', '1-x', '2', '4', 'x, 'd. contacting the high boiling temperature fraction with a gaseousoxidizing agent and an oxidizing catalyst having a formula CuZnAlOwherein x ranges from 0 to 1 to convert refractory organosulfur compounds including dibenzothiophenes, alkyl derivatives of dibenzothiophenes and long-chain alkylated derivatives of benzothiophene having a boiling point in the range of the high boiling temperature fraction, to SOby breaking the C—S bonds.'}2. The method of claim 1 , wherein the oxidizing catalyst ...

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Номер записи: 72

15-08-2013 дата публикации

WASTE HEAT RECOVERY SYSTEM AND METHOD OF OPERATING THE SAME

Номер: US20130205776A1

Автор: JR. Eric P., Steinbach, Yin JianMin

Принадлежит: MODINE MANUFACTURING COMPANY

A waste heat recovery system includes a hot gas stream flow path, a pump, an expander, a first working fluid flow path fluidly connecting a pump outlet and an expander inlet, a second working fluid flow path fluidly connecting an expander outlet and a pump inlet, a first heat exchange section that transfers heat from the hot gas stream to working fluid traveling along the first working fluid flow path, a second heat exchange that transfers heat from the hot gas stream to working fluid traveling along the first working fluid flow path between the pump and the first heat exchange section, and a third working fluid flow path fluidly connecting a first point of the first working fluid path to a second point of the second working fluid path to permit at least a portion of the working fluid to bypass the first heat exchange section and the expander. 1. A waste heat recovery system to generate power from thermal energy contained in a hot gas stream , comprising:a hot gas stream flow path extending from a hot gas stream source and along which the hot gas stream flows;a pump;an expander;a first working fluid flow path fluidly connecting an outlet of the pump and an inlet of the expander;a second working fluid flow path fluidly connecting an outlet of the expander and an inlet of the pump;a first heat exchange section located along both the first working fluid flow path and the hot gas stream flow path to transfer heat from the hot gas stream to working fluid traveling along the first working fluid flow path;a second heat exchange section located along both the first working fluid flow path and the hot gas stream flow path to transfer heat from the hot gas stream to working fluid traveling along the first working fluid flow path between the pump and the first heat exchange section; anda third working fluid flow path fluidly connecting a first branch point along the first working fluid path to a second branch point along the second working fluid path to enable at least a ...

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Номер записи: 73

15-08-2013 дата публикации

Method for Producing Diesel Fuel with Improved Yield and Quality by Integration of Fluidized Catalytic Cracking (FCC) and Hydrocracking (HC)

Номер: US20130206644A1

Автор: GALDEANO Ruben, GUZMAN Adrian, MENDIONDO Hugo

Принадлежит: YPF S.A.

A method for producing diesel fuel with improved yield and quality by integration of fluidized catalytic cracking (FCC) and hydrocracking (HC), comprising the following stages: 1. A method for producing diesel fuel with improved yield and quality by integration of fluidized catalytic cracking (FCC) and hydrocracking (HC) , comprising the following stages:a. arrangement of FCC and HC processes in parallel;b. feedstock segregation to each of such processes depending on the content of aromatic hydrocarbons; andc. a common fractioning stage for both output streams from HC and FCC processes, also comprising recycling the unconverted fraction towards the FCC unit.2. Method according to claim 1 , wherein at least a portion of the hydrocracking reactor effluent is used to preheat the feed to the same reactor claim 1 , thus reducing its temperature before mixing with the FCC unit effluent and entering the common fractioning stage.3. Method according to claim 1 , wherein said common fractioning stage for both output streams from HC and FCC processes claim 1 , comprises recycling the unconverted heavy gasoil to the riser of the FCC unit and recycling the decanted gasoil to the HC unit.4. Method according to claim 1 , wherein said common fractioning stage for both output streams from HC and FCC processes claim 1 , comprises optionally recycling a portion of the decanted gasoil stream to the HC unit claim 1 , comprises mixing the remaining portion or the whole of said stream with the unconverted heavy gasoil claim 1 , and comprises recycling the resulting mixed stream to extinction towards the riser of the FCC unit claim 1 , thus allowing control of the carbon balance in the FCC unit.5. Method according to claim 1 , wherein the temperature of the hydrocracking reactor effluent is between 300° C. and 390° C.6. Method according to claim 1 , wherein the temperature of the FCC reactor effluent is between 500° C. and 580° C.7. Method according to claim 1 , wherein the hydrocracking ...

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Номер записи: 74

15-08-2013 дата публикации

PROCESS FOR CONVERTING A HEAVY FEED USING A CATALYTIC CRACKING UNIT AND A STEP FOR SELECTIVE HYDROGENATION OF THE GASOLINE OBTAINED FROM CATALYTIC CRACKING

Номер: US20130211161A1

Автор: DULOT Hugues, Feugnet Frederic, HUGUES Francois, PUCCI Annick, Touchais Natacha

Принадлежит: IFP ENERGIES NOUVELLES

The present invention describes a process for converting a heavy feed which is flexible for the production of propylene, gasoline and middle distillate. 1. A process for converting a heavy hydrocarbon feed having great flexibility for the production of propylene , gasoline and middle distillate , carrying out the following steps when the process operates in maxi propylene mode:a) a step for catalytic cracking (FCC) of the heavy cut, producing a C5-220° C. gasoline cut when the FCC is orientated towards the production of gasoline and C5-150° C. when the FCC is orientated towards the production of middle distillate;{'sup': −1', '−1, 'b) a step for selective hydrogenation (SHU) of the gasoline cut obtained from the catalytic cracking unit (FCC), operating under the following conditions: a pressure in the range 0.5 to 5 MPa, a temperature in the range 80° C. to 220° C., with a liquid hourly space velocity (LHSV) in the range 1 hto 10 h, the liquid hourly space velocity being expressed in litres of feed per litre of catalyst per hour (L/L·h);'}c) a step for separating the gasoline obtained from step b) by distillation (SPLIT) in order to separate two cuts: a light C5-Pf gasoline cut and a heavy Pf-220° C. gasoline cut, the temperature Pf, being the boundary between light gasoline and heavy gasoline, being in the range 50° C. to 150° C., preferably in the range 50° C. to 100° C., and more preferably in the range 50° C. to 80° C.;d) a step for purification (PUR) of the light C5-Pf gasoline obtained from step c) which is intended to reduce the nitrogen to less than 1 ppm by weight, preferably less than 0.2 ppm; temperature in the range 60° C. to 350° C., preferably in the range 100° C. to 300° C., and still more preferably in the range 120° C. to 250° C.;', {'sup': '6', 'pressure in the range 1 to 10 MPa (1 MPa=10Pascal), preferably in the range 2 to 8 MPa, and more preferably in the range 3 to 6 MPa;'}, 'catalysts based on silica-alumina or amorphous aluminosilicate, or ...

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Номер записи: 75

15-08-2013 дата публикации

CATALYTIC CONVERSION METHOD FOR IMPROVING PRODUCT DISTRIBUTION

Номер: US20130211167A1

Автор: CUI Shouye, Jiang Nan, Liu Siwei, Liu Yinliang, XU Youhao

Принадлежит: CHINA PETROLEUM & CHEMICAL CORPORATION

The present invention relates to a catalytic conversion process for improving the product distribution, characterized in that a feedstock oil of good quality is contacted with a hot regenerated catalyst having a lower activity in a reactor to carry out a cracking reaction, the reaction product is separated from the spent catalyst to be regenerated, then the reaction product is fed into a separation system, and the spent catalyst to be regenerated is stripped, regenerated and recycled in the process. The isobutene content in the liquefied petroleum gas (LPG) produced by the process is increased by a factor of more than 30%, and the olefin content in the gasoline composition may be increased to more than 30 wt. %. The product distribution is optimized, and the yields of dry gas and coke are decreased, so as to sufficiently utilize the petroleum resources. 1. A catalytic conversion process for improving the product distribution , characterized in that a feedstock oil of good quality is contacted with a hot regenerated catalyst having a lower activity in a reactor to carry out a cracking reaction , the reaction product is separated from the spent catalyst to be regenerated , then the reaction product is fed into a separation system , and the spent catalyst to be regenerated is stripped , regenerated and recycled in the process , wherein said catalytic conversion process is used to increase the isobutene content in the liquefied petroleum gas and the olefin content in the gasoline in the industrial FCC process.2. The process according to claim 1 , characterized in that the feedstock oil of good quality is contacted with the hot regenerated catalyst having a lower activity in the lower part of the reactor to carry out a cracking reaction claim 1 , followed by a selective hydrogen transfer reaction and isomerization reaction during the upward movement of the cracking reaction product and coke-containing catalyst claim 1 , the product of the selective hydrogen transfer ...

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Номер записи: 76

29-08-2013 дата публикации

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

Номер: US20130220884A1

Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, SAYED Essam, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

A process is provided that is directed to a steam pyrolysis zone integrated with a hydrotreating zone and a solvent deasphalting zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. The integrated hydrotreating, solvent deasphalting and steam pyrolysis process comprises charging the crude oil to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity; charging the hydroprocessed effluent to a solvent deasphalting zone with an effective amount of solvent to produce a deasphalted and demetalized oil stream and a bottom asphalt phase; thermally cracking the deasphalted and demetalized oil stream in the presence of steam to produce a mixed product stream; separating the mixed product stream; purifying hydrogen recovered from the mixed product stream and recycling it to the hydroprocessing zone; recovering olefins and aromatics from the separated mixed product stream; and recovering pyrolysis fuel oil from the separated mixed product stream. 1. An integrated hydrotreating , solvent deasphalting and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals , the process comprising:a. charging the crude oil to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity;b. charging the hydroprocessed effluent to a solvent deasphalting zone with an effective amount of solvent to produce a deasphalted and demetalized oil stream and a bottom asphalt phase;c. thermally cracking the deasphalted and demetalized oil stream in the presence of ...

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Номер записи: 77

29-08-2013 дата публикации

Catalyst for selective oxidation of nh3 to n2 and method for preparing the same

Номер: US20130224090A1

Автор: Gi Ho Goh, Hong Seok Jung, Seong Ho Lee, Seung Hoon Oh, Sung Hwan Kim, Woo Jin Lee, Yong Woo Kim, Young Eun Cheon

Принадлежит: SK Innovation Co Ltd

Disclosed is a catalyst which can convert ammonia contained in exhaust gas from an engine of a vehicle equipped with a Urea-SCR (Urea-Selective Catalytic Reduction) system, to nitrogen, and a method for preparating the same. The catalyst can convert ammonia which is failed to participate in a conversion reaction of NOx to N2 and slipped out of the SCR catalyst, to nitrogen via a SCO (Selective Catalytic Oxidation) reaction, before the ammonia is released to the air.

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Номер записи: 78

29-08-2013 дата публикации

Methods for making and distributing batches of butane-enriched gasoline

Номер: US20130225883A1

Автор: Larry D. Mattingly, Steven M. Vanderbur

Принадлежит: SUNOCO PARTNERS BUTANE BLENDING LLC

Disclosed are automated methods and systems for certifying the volatility of butane-enriched gasoline downstream of a butane blending operation. Such automated methods and systems provide significant advantages to comply with volatility requirements imposed by EPA or state regulations.

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Номер записи: 79

05-09-2013 дата публикации

Integrated hydrotreating and steam pyrolysis process including hydrogen redistribution for direct processing of a crude oil

Номер: US20130228495A1

Автор: Abdennour Bourane, Abdul Rahman Zafer AKHRAS, Ibrahim A. ABBA, Raheel Shafi

Принадлежит: Saudi Arabian Oil Co

Steam pyrolysis and hydroprocessing are integrated including hydrogen redistribution to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. A feed is initially split into a light portion and a heavy portion, and the heavy portion is hydroprocessed. A hydroprocessed effluent is charged, along with steam, to a convection section of a steam pyrolysis zone. The mixture is heated and passed to a vapor-liquid separation section. A residual portion is removed and light components are charged to a pyrolysis section of the steam pyrolysis zone. A mixed product stream is recovered from the steam pyrolysis zone and it is separated into product including olefins and aromatics.

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Номер записи: 80

12-09-2013 дата публикации

Upgrading Hydrocarbon Pyrolysis Products

Номер: US20130233764A1

Автор: Ananthakrishnan Bhasker, Keith G. Reed, S. Mark Davis, Stephen H. Brown, Teng Xu

Принадлежит: ExxonMobil Chemical Patents Inc

The invention relates to upgraded pyrolysis products, processes for upgrading products obtained from hydrocarbon pyrolysis, equipment useful for such processes, and the use of upgraded pyrolysis products.

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Номер записи: 81

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: 82

12-09-2013 дата публикации

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

Номер: US20130233766A1

Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, HASSELMEYER Julio, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

An integrated hydrotreating and steam pyrolysis process for the direct processing of a crude oil is provided to produce olefinic and aromatic petrochemicals. Crude oil and hydrogen are charged to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity. Hydroprocessed effluent is thermally cracked in the presence of steam to produce a mixed product stream, which is separated. Hydrogen from the mixed product stream is purified and recycled to the hydroprocessing zone, and olefins and aromatics are recovered from the separated mixed product stream. 1. An integrated hydrotreating and steam pyrolysis process for the direct processing of crude oil to produce olefinic and aromatic petrochemicals , the process comprising:a. charging the crude oil and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity;b. thermally cracking hydroprocessed effluent in the presence of steam in a steam pyrolysis zone to produce a mixed product stream;c. separating the thermally cracked mixed product stream into hydrogen, olefins, aromatics and pyrolysis fuel oil;d. purifying hydrogen recovered in step (c) and recycling it to step (a);e. recovering olefins and aromatics from the separated mixed product stream; andf. recovering pyrolysis fuel oil from the separated mixed product stream.2. The integrated process of claim 1 , further comprising separating the hydroprocessed effluent from the hydroprocessing zone into a heavy fraction and a light fraction in a hydroprocessed effluent separation zone claim 1 , wherein the light fraction is the hydroprocessed effluent ...

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Номер записи: 83

12-09-2013 дата публикации

INTEGRATED HYDROTREATING AND STEAM PYROLYSIS PROCESS INCLUDING RESIDUAL BYPASS FOR DIRECT PROCESSING OF A CRUDE OIL

Номер: US20130233767A1

Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

A process is provided that is directed to a steam pyrolysis zone integrated with a hydroprocessing zone including residual bypass to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. The integrated hydrotreating and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals comprises separating the crude oil into light components and heavy components; charging the light components and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity; thermally cracking the hydroprocessed effluent in the presence of steam to produce a mixed product stream; separating the mixed product stream; purifying hydrogen recovered from the mixed product stream and recycling it to the hydroprocessing zone; recovering olefins and aromatics from the separated mixed product stream; and recovering a combined stream of pyrolysis fuel oil from the separated mixed product stream and heavy components from step (a) as a fuel oil blend. 1. An integrated hydrotreating and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals , the process comprising:a. separating the crude oil into light components and heavy components;b. charging the light components and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity;c. thermally cracking hydroprocessed effluent in the presence of steam to produce a mixed product stream;d. separating the thermally cracked mixed product stream;e. purifying ...

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Номер записи: 84

12-09-2013 дата публикации

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

Номер: US20130233768A1

Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, SAYED Essam, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

A process is provided that is directed to a steam pyrolysis zone integrated with a solvent deasphalting zone and a hydrotreating zone to permit direct processing of crude oil feedstocks to produce petrochemicals including olefins and aromatics. The integrated solvent deasphalting, hydrotreating and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals comprises: charging the crude oil to a solvent deasphalting zone with an effective amount of solvent for producing a deasphalted and demetalized oil stream and a bottom asphalt phase; charging the deasphalted and demetalized oil stream and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity; thermally cracking the hydroprocessed effluent in the presence of steam to produce a mixed product stream; separating the mixed product stream; purifying hydrogen recovered from the mixed product stream and recycling it to the hydroprocessing zone; recovering olefins and aromatics from the separated mixed product stream; and recovering pyrolysis fuel oil from the separated mixed product stream. 1. An integrated solvent deasphalting , hydrotreating and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals , the process comprising:a. charging the crude oil to a solvent deasphalting zone with an effective amount of solvent for producing a deasphalted and demetalized oil stream and a bottom asphalt phase;b. charging the deasphalted and demetalized oil stream and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent reduced having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and ...

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Номер записи: 85

19-09-2013 дата публикации

EXPANSION OF FUEL STREAMS USING MIXED HYDROCARBONS

Номер: US20130239470A1

Автор: BUCHANAN Keith D.

Принадлежит: SUNOCO PARTNERS BUTANE BLENDING LLC

Methods and systems for blending multiple batches of mixed hydrocarbons into fuel streams downstream of the refinery are provided that do not compromise the octane value of the fuel and do not cause the volatility of the fuel to exceed volatilities imposed by government regulation. 2) A method for making mixed pentane enriched fuel without depressing the octane of the fuel , comprising the steps: i) a first enclosed conduit transmitting a fuel stream,', 'ii) a second enclosed conduit transmitting an additive stream, wherein the additive stream comprises mixed pentanes, and', 'i) an outlet in the second enclosed conduit forming a fluid connection with an inlet in the first enclosed conduit,, 'a) providing a fuel blending unit characterized by i) a volatility for the additive stream (the “additive stream volatility”),', 'ii) a flow rate for the fuel stream (the “fuel stream flow rate”),', 'iii) an octane value for the fuel stream (the “fuel stream octane value”), and, 'b) providingiv) a maximum blended volatility for the fuel stream (the “maximum blended volatility”),c) measuring the fuel stream for its actual volatility (the “fuel stream volatility”), i) the fuel stream volatility,', 'ii) the additive stream volatility, and', 'iii) the fuel stream flow rate,, 'd) calculating a rate (the “additive stream flow rate”) at which the additive stream can be added to the fuel stream so as not to exceed the maximum blended volatility, wherein the calculating is based upone) adding the additive stream to the fuel stream at the additive stream flow rate at the fluid connection to make pentane enriched fuel, andf) adding ethanol to the pentane enriched fuel in an amount sufficient to overcome the depression in octane caused by n-pentane in the mixed pentanes.3) A method for blending heterogeneous batches of mixtures of light hydrocarbons into a primary fuel stream (the “fuel stream”) comprising: i) a mixed hydrocarbon stream (the “additive stream”) comprising a plurality of ...

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Номер записи: 86

19-09-2013 дата публикации

PROCESS FOR DEEP DESULFURIZATION OF CRACKED GASOLINE WITH MINIMUM OCTANE LOSS

Номер: US20130240405A1

Автор: Chopra Anju, Kumar Brijesh, Kumar Sarvesh, Malhotra Kumar Ravinder, Rajagopal Santanam, Sharma Alok

Принадлежит: INDIAN OIL CORPORATION LIMITED

The present invention provides a process for deep desulphurization of cracked gasoline with minimum octane loss of about 1-2 units. In this process full range cracked gasoline from FCC, Coker, Visbreaker etc is sent to Diolefin Saturation Reactor for selective saturation of diolefins. After saturation of diolefins, the stream is sent to Splitter for splitting into three cuts i.e Light Cut (IBP-70° C.), Intermediate Cut (70-90° C.) and Heavy Cut (90-210° C.). The Light Cut which contains majority of the high octane olefins and mercaptan sulfur is desulfurized with caustic treatment using Continuous Film Contactor (CFC). The sulfur in the Intermediate Cut is also predominantly mercaptans and the cut can be desulfurised by caustic treatment using CFC along with Light cut or separately desulfurised before being sent for isomerization. The Heavy Cut containing mainly thiophinic sulfur compounds is treated either by using conventional HDS process or reactive adsorption process. 2. The process as claimed in claim 1 , wherein the diolefins content is reduced to a level less than 0.05% and preferably below 0.02%.3. The process as claimed in claims 1 , wherein the different cuts are as under:i. light cut preferably IBP-90° C., most preferably IBP-70° C.;ii. intermediate cut preferably 70-120° C., most preferably 70-90° C.;iii. heavy cut preferably 70-210° C., most preferably between 90 and 210° C.4. The process as claimed in claims 1 , wherein intermediate and/or heavy cuts are subjected to catalytic treatment claims 1 , the catalyst being CoMo or NiMo catalyst claims 1 , at a pressure in the range 10 to 30 bar claims 1 , temperature in the range of 250 to 300° C. claims 1 , hydrogen to hydrocarbon ratio varying between 20 to 200 depending on sulfur and olefin content in the feed claims 1 , to reduce sulfur preferably below 30 ppm claims 1 , more preferably below 10 ppm and most preferably below 5 ppm and blended in gasoline.5. The process as claimed in claim 1 , wherein ...

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Номер записи: 87

19-09-2013 дата публикации

INTEGRATION OF SOLVENT DEASPHALTING WITH RESIN HYDROPROCESSING AND WITH DELAYED COKING

Номер: US20130240407A1

Автор: Gillis Daniel B.

Принадлежит: Foster Wheeler USA Corporation

The invention is directed to a process that combines the solvent deasphalting with resin hydrotreatment and coupled with delayed coking so as to reduce the costs associated with performing each of the steps separately. The integrated process of the invention permits higher product yields coupled with lower energy and transportation costs. 1. A process for deasphalting a solvent comprising:introducing a hydrocarbon oil feedstock to a reactor;introducing a solvent to the feedstock;separating an asphaltene-containing fraction from the feedstock to form an asphaltene depleted feedstock;separating a resin-containing fraction in a resin recovery section from the asphaltene separated feedstock to form a resin depleted feedstock;separating a deasphalted oil-containing fraction from the resin depleted feedstock;integrating the resin recovery section with a hydroprocessing process;hydroprocessing the resin-containing fraction in the hydroprocessing process to generate a hydroprocessed residue product; andprocessing the hydroprocessed residue product in a delayed coker2. The process of claim 1 , wherein the hydroprocessing process is carried out at hydrogen partial pressures ranging from about 800 to about 2500 psig.3. The process of claim 1 , wherein the hydroprocessing process is carried out at temperatures ranging from about 650 to about 930° F.4. The process of claim 1 , wherein the hydroprocessing process is carried out with a catalyst.5. The process of claim 4 , wherein the catalyst is a metal catalyst.6. The process of claim 5 , wherein the metal catalyst comprises one or more metals selected from the group consisting of iron claim 5 , nickel claim 5 , molybdenum and cobalt.7. The process of claim 1 , wherein the hydroprocessed residue product is subjected to a further separation process.8. The process of wherein the further separation process comprises generating a resin overhead stream and a resin bottoms stream.9. The process of wherein the solvent comprises a light ...

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Номер записи: 88

26-09-2013 дата публикации

INTEGRATED HYDROPROCESSING AND STEAM PYROLYSIS OF CRUDE OIL TO PRODUCE LIGHT OLEFINS AND COKE

Номер: US20130248416A1

Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, SAYED Essam, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

An integrated hydrotreating, steam pyrolysis and coker process for the direct processing of a crude oil is provided to produce olefinic and aromatic petrochemicals, and petroleum coke. Crude oil and recycled coker liquid product are charged to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent which is thermally cracked in the presence of steam to produce a mixed product stream. The residual liquid fraction recovered upstream of the thermal cracking unit or within the thermal cracking unit is thermally cracked under conditions effective to produce coke and coker liquid product. The coker liquid product is recycled to the step of hydroprocessing while the petroleum coke is recovered. Hydrogen from the mixed product stream is purified and recycled to the hydroprocessing zone, and olefins, aromatics and pyrolysis fuel oil are recovered from the separated mixed product stream. 1. An integrated hydroprocessing , steam pyrolysis and coker process for production of petroleum coke and olefinic and aromatic petrochemicals from a crude oil feed , the process comprising:a. hydroprocessing the crude oil and a coker liquid product in the presence of hydrogen under conditions effective to produce a hydroprocessed effluent having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity;b. thermally cracking the hydroprocessed effluent in the presence of steam in a steam pyrolysis zone by heating the hydroprocessed effluent in a convection section of a steam pyrolysis zone, separating the heated hydroprocessed effluent into a vapor fraction and a residual liquid fraction, and passing the vapor fraction to a pyrolysis section operating under conditions effective to produce a mixed product stream;c. thermally cracking the residual liquid fraction under conditions effective to produce coke and the coker liquid product, wherein the coker ...

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Номер записи: 89

26-09-2013 дата публикации

INTEGRATED HYDROPROCESSING, STEAM PYROLYSIS AND SLURRY HYDROPROCESSING OF CRUDE OIL TO PRODUCE PETROCHEMICALS

Номер: US20130248417A1

Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, SAYED Esam, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

Crude oil is charged to a hydroprocessing zone in the presence of hydrogen operating under conditions effective to produce a hydroprocessed effluent, which is thermally cracked in the presence of steam in a steam pyrolysis zone to produce a mixed product stream. Heavy components, which are derived from one or more of the hydroprocessed effluent, a heated stream within the steam pyrolysis zone, or the mixed product stream catalytically cracking are charged to a slurry hydroprocessing zone to produce a slurry intermediate product which is then thermally cracked. Olefins and aromatics are recovered from the separated mixed product stream as product. 1. An integrated hydroprocessing , steam pyrolysis and slurry hydroprocessing process for direct conversion of crude oil to produce olefinic and aromatic petrochemicals , the process comprising:a. hydroprocessing the crude oil and a slurry process product in the presence of hydrogen under conditions effective to produce a hydroprocessed effluent having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity;b. thermally cracking hydroprocessed effluent in the presence of steam in a steam pyrolysis zone under conditions effective to produce a mixed product stream;c. processing heavy components derived from one or more of the hydroprocessed effluent, a heated stream within the steam pyrolysis zone, or the mixed product stream, in a slurry hydroprocessing zone to produce slurry intermediate product;d. conveying the slurry intermediate product to the step of thermally cracking;e. separating a combined product stream including thermally cracked product and slurry intermediate product;f. purifying hydrogen recovered in step (e) and recycling it to the step of hydroprocessing; andg. recovering olefins and aromatics from the separated combined product stream.2. The integrated process of claim 1 , further comprising recovering ...

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Номер записи: 90

26-09-2013 дата публикации

INTEGRATED SLURRY HYDROPROCESSING AND STEAM PYROLYSIS OF CRUDE OIL TO PRODUCE PETROCHEMICALS

Номер: US20130248418A1

Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, SAYED Esam, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

An integrated slurry hydroprocessing and steam pyrolosyis process for the production of olefins and aromatic petrochemicals from a crude oil feedstock is provided. Crude oil, a steam pyrolysis residual liquid fraction and slurry reside are combined and treated in a hydroprocessing zone in the presence of hydrogen under conditions effective to produce an effluent having an increased hydrogen content. The effluent is thermally cracked with steam under conditions effective to produce a mixed product stream and steam pyrolysis residual liquid fraction. The mixed product stream is separated and olefins and aromatics are recovered and hydrogen is purified and recycled. 1. An integrated slurry hydroprocessing and steam pyrolysis process for production of olefinic and aromatic petrochemicals from crude oil , the process comprising:a. treating the crude oil and heavy components derived from one or more of slurry residue, a heated stream within the steam pyrolysis zone or a mixed product stream, in a slurry hydroprocessing zone in the presence of hydrogen under conditions effective to produce an effluent having an increased hydrogen content;b. thermally cracking the effluent in the presence of steam in a steam pyrolysis zone under conditions effective to produce a mixed product stream;c. separating the mixed product stream;d. purifying hydrogen recovered in step (c) and recycling it to step (a); ande. recovering olefins and aromatics from the separated mixed product stream.2. The integrated process of claim 1 , further comprising recovering pyrolysis fuel oil from the separated mixed product stream for use as at least a portion of the heavy components processed in step (a).3. The integrated process of claim 1 , further comprising separating the effluent from step (a) into a vapor phase and a liquid phase in a vapor-liquid separation zone claim 1 , wherein the vapor phase is thermally cracked in step (b) claim 1 , and at least a portion of the liquid phase is recycled as ...

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Номер записи: 91

26-09-2013 дата публикации

INTEGRATED HYDROPROCESSING, STEAM PYROLYSIS AND CATALYTIC CRACKING PROCESS TO PRODUCE PETROCHEMICALS FROM CRUDE OIL

Номер: US20130248419A1

Автор: ABBA Ibrahim A., AKHRAS Abdul Rahman Zafer, BOURANE Abdennour, SAYED Essam, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

An integrated hydrotreating, steam pyrolysis and catalytic cracking process for the production of olefins and aromatic petrochemicals from a crude oil feedstock is provided. Crude oil and hydrogen are charged to a hydroprocessing zone under conditions effective to produce a hydroprocessed effluent, which is thermally cracked in the presence of steam in a steam pyrolysis zone to produce a mixed product stream. Heavy components are catalytically cracked, which are derived from one or more of the hydroprocessed effluent, a heated stream within the steam pyrolysis zone, or the mixed product stream catalytically cracking. Catalytically cracked products are produced, which are combined with the mixed product stream and the combined stream is separated, and olefins and aromatics are recovered as product streams. 1. An integrated hydroprocessing , steam pyrolysis and catalytic cracking process for production of olefinic and aromatic petrochemicals from a crude oil feed , the process comprising:a. charging the crude oil and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity;b. thermally cracking hydroprocessed effluent in the presence of steam in a steam pyrolysis zone to produce a mixed product stream;c. catalytically cracking heavy components derived from one or more of the hydroprocessed effluent, a heated stream within the steam pyrolysis zone, or the mixed product stream, to produce catalytically cracked products;d. separating a combined product stream including thermally cracked products and catalytically cracked products;e. purifying hydrogen recovered in step (d) and recycling it to step (a); andf. recovering olefins and aromatics from the separated combined product stream.2. The integrated process of claim 1 , further comprising recovering ...

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Номер записи: 92

26-09-2013 дата публикации

INTEGRATED HYDROPROCESSING AND FLUID CATALYTIC CRACKING FOR PROCESSING OF A CRUDE OIL

Номер: US20130248421A1

Автор: ABBA Ibrahim A., BOURANE Abdennour, SAYED Essam, SHAFI Raheel

Принадлежит: Saudi Arabian Oil Company

An integrated hydroprocessing and fluid catalytic cracking process is provided for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals. Crude oil and hydrogen are charged to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent having a reduced content of contaminants, an increased paraffinicity, reduced Bureau of Mines Correlation Index, and an increased American Petroleum Institute gravity. The hydroprocessed effluent is separated into a low boiling fraction and a high boiling fraction. The low boiling fraction is cracked in a first downflow reactor of a fluid catalytic cracking unit in the presence of a predetermined amount of catalyst to produce cracked products and spent catalyst, and the high boiling fraction is cracked in a second downflow reactor of the fluid catalytic cracking unit in the presence of a predetermined amount of catalyst to produce cracked products and spent catalyst. Spent catalyst from both the first and second downflow reactors are regenerated in a common regeneration zone, and first and second cracked product streams are recovered. 1. An integrated hydroprocessing and fluid catalytic cracking process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals , the process comprising:a. charging the crude oil and hydrogen to a hydroprocessing zone operating under conditions effective to produce a hydroprocessed effluent having a reduced content of contaminants, an increased paraffinicity and an increased American Petroleum Institute gravity;b. separating the hydroprocessed effluent into a low boiling fraction and a high boiling fraction;c. cracking the low boiling fraction in a first downflow reactor of a fluid catalytic cracking unit in the presence of a predetermined amount of catalyst to produce cracked products and spent catalyst;d. cracking the high boiling fraction in a second downflow reactor of the fluid catalytic cracking unit ...

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Номер записи: 93

26-09-2013 дата публикации

HIGH PERFORMANCE LIQUID ROCKET PROPELLANT

Номер: US20130253237A1

Автор: Mathur Indresh

Принадлежит: Johann Haltermann Limited

Disclosed is a high performance hydrocarbon fuel characterized by a hydrogen content greater than 14.3% by weight, a hydrogen to carbon atomic ratio greater than 2.0 and/or a heat of combustion greater than 18.7 KBtu/lb. The disclosed fuels generally have a paraffin content that is at least 90% by mass and a C-Cisoparaffin content of at least 40% by mass. 1. A hydrocarbon fuel having a range of components that provide a boiling point range of at least 100° F. , and having a hydrogen content greater than 14.3% on a mass basis.2. A hydrocarbon fuel having a range of components that provide a boiling point range of at least 100° F. , and having a hydrogen to carbon ratio greater than 2.0 on an atomic basis.3. The hydrocarbon fuel of having a net heat of combustion greater than 18.7 KBtu/lb.4. A hydrocarbon fuel in accordance with which is a blend of an isoparaffin and a highly paraffinic kerosene.5. The hydrocarbon fuel of claim 4 , in which the isoparaffin is comprised of at least one isododecane claim 4 , at least one isohexadecane claim 4 , at least one isoeicosane claim 4 , or a mixture of these.6. A hydrocarbon fuel in accordance with which is a blend of an isoparaffin and a naphthenic kerosene.7. The hydrocarbon fuel of claim 6 , in which the isoparaffin is comprised of at least one isododecane claim 6 , at least one isohexadecane claim 6 , at least one isoeicosane claim 6 , or a mixture of these.8. (canceled)9. (canceled)10. A fuel composition comprising:a total paraffin content of at least 90% by mass; andwherein the composition contains at least 40% by mass of isoparaffins having from 12 to 20 carbon atoms.11. The composition of claim 10 , in which a net heat of combustion is greater than 18 claim 10 ,700 BTU/lb.12. The composition of claim 10 , in which the hydrogen content is greater than 14.5% by mass.13. The composition of wherein the total paraffin content is at least 95% by mass.14. The composition of wherein the composition contains at least 60% by mass ...

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Номер записи: 94

26-09-2013 дата публикации

METHOD FOR PRODUCING LUBRICATING BASE OIL WITH LOW CLOUD POINT AND HIGH VISCOSITY INDEX

Номер: US20130253238A1

Автор: Chi Kebin, Gao Shanbin, Hu Sheng, Li Wenle, Liu Yanfeng, Meng Xiangbin, Tan Mingwei, Tian Zhijian, Wang Bingchun, Wang Lei, Xu Yunpeng, Yan Lijun, Zhu Jinling

Принадлежит:

The present invention relates to a method for producing lubricating base oil with a low cloud point and a high viscosity index. In the method, a lubricating base oil with a low pour point, a low cloud point and a high viscosity index is produced by a hydrorefining-isomerization/asymmetrical cracking-hydrofinishing in the presence of hydrogen, wherein a highly waxy heavy fraction oil having an initial boiling point of 300° C. to 460° C., a wax content of 5% or more, a pour point of −20° C. or more and a cloud point of −5° C. or more is used as a raw material, and naphtha and middle fraction oil being co-produced. The method is characterized mainly in the high yield of heavy base oil, a low pour point and cloud point, a high viscosity and viscosity index of the base oil. 1. A method for producing a lubricating base oil with a low cloud point and a high viscosity index , wherein the cloud point is lower than −5° C. , and the viscosity index is higher than 120 , the method comprises: producing a lubricating base oil by a hydrorefining-isomerization/asymmetrical cracking-hydrofinishing in the presence of hydrogen , wherein a highly waxy heavy fraction oil having an initial boiling point of 300° C. to 460° C. , a wax content of 5% or more , a pour point of −20° C. or more and a cloud point of −5° C. or more is used as a raw material;(1) during the hydrorefining process, a wax-containing heavy feed stock contacts a pre-refining catalyst, and is subjected to desulfurization, denitrogenation, aromatic saturation and a ring-opening reaction, a light product generated in the hydrorefining process is separated by a stripping column as a byproduct, and a heavy product enters an isomerization-asymmetrical cracking process;{'sup': −1', '−1', '3', '3', '3', '3, 'the operating conditions of the hydrorefining process are: reaction temperature: 350° C. to 410° C., hydrogen partial pressure: 10 MPa to 18 MPa, space velocity: 0.5 hto 2.0 h, volume ratio of hydrogen to oil:300 Nm/mto ...

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Номер записи: 95

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: 96

10-10-2013 дата публикации

HIGH VISCOSITY HIGH QUALITY GROUP II LUBE BASE STOCKS

Номер: US20130264246A1

Автор: Baker Charles L., Dandekar Ajit B., Fingland Bradley R., Hagee Bryan E., Holtzer Gretchen L., Pathare Rugved Prakash, Sanchez Eugenio, WANG Frank C., Yung Cathleen

Принадлежит: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY

Provided are high viscosity high quality Group II lube base stocks with improved properties produced by an integrated hydrocracking and dewaxing process. In one form, the Group II lube base stock includes greater than or equal to 90 wt. % saturates, and less than 10 wt. % aromatics, and has an aromatic performance ratio between 1.0 and 5.0. Also provided are lubricant formulations including the high viscosity high quality Group II lube base stock. 1. A Group II lube basestock comprising from greater than or equal to 90 wt. % saturates , and less than 10 wt. % aromatics , and having an aromatic performance ratio between 1.0 and 5.0.2. The tube base stock of claim 1 , wherein the aromatic performance ratio between 1.0 and 3.0.3. The lube base stock of claim 1 , wherein the aromatic performance ratio between 1.5 and 3.5.4. The lube base stock of claim 1 , wherein the saturates are greater than or equal to 95 wt. %.5. The lube base stock of claim 1 , wherein the kinematic viscosity at 100 deg. C. is between 4.0 and 6.0 cSt claim 1 , and wherein the UV absorptivity at a wavelength between 280 nm and 320 nm is between 0.015 and 0.07 l/g-cm.6. The lube base stock of claim 5 , wherein the UV absorptivity at a wavelength between 280 nm and 320 nm is between 0.02 and 0.065 l/g-cm.7. The lube base stock of claim 6 , wherein the UV absorptivity at a wavelength between 280 nm and 320 nm is between 0.03 and 0.05 l/g-cm.8. The lube base stock of claim 1 , wherein the kinematic viscosity at 100 deg. C. is between 6.0 and 112.0 cSt claim 1 , and wherein the UV absorptivity at a wavelength between 260 nm and 320 nm is between 0.001 and 0.02 l/g-cm.9. The lube base stock of further including naphtheno-aromatics and claim 1 , wherein the 3-4+ ring species of the aromatics and the naphtheno-aromatics ranges from 20 to 85 wt. % of the total aromatics and the naptheno-aromatics.10. The lube base stock of claim 9 , wherein the 3-4+ ring species of the aromatics and the naphtheno-aromatics ...

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Номер записи: 97

10-10-2013 дата публикации

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

Номер: US20130267749A1

Автор: Masahide Kobayashi, Shinichiro Yanagawa, Yasuyuki Iwasa

Принадлежит: JX Nippon Oil and Energy Corp

The catalyst for producing monocyclic aromatic hydrocarbons is for producing monocyclic aromatic hydrocarbons having 6 to 8 carbon number from oil feedstock having a 10 volume % distillation temperature of 140° C. or higher and a 90 volume % distillation temperature of 380° C. or lower. The catalyst includes crystalline aluminosilicate, phosphorus, and a binder, and the amount of phosphorus is 0.1 to 10 mass % based on the total mass of the catalyst.

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Номер записи: 98

17-10-2013 дата публикации

FUEL COMPOSITION

Номер: US20130269243A1

Автор: Lund Morten A.

Принадлежит:

A fuel composition for use in an internal combustion engine comprising at least one liquid fuel and at least one gaseous fuel, the gaseous fuel having an effective solubility in the liquid fuel at twenty degrees Celsius and one atmosphere in the range of 0.0000001 g/kg to 0.0002 g/kg, wherein dispersion of the gaseous fuel within the liquid fuel before introduction of the fuel composition to the injection system of the engine is such that molecules of the liquid and gaseous fuels are substantially equidistant one from another, liquid from liquid and gas from gas, within a variance preferably of no more than one hundred percent (±100%), more preferably of no more than fifty percent (±50%), and most preferably of no more than twenty-five percent (±25%), whereby the fuel composition is substantially homogeneous so as to promote the atomization of the liquid fuel and thus improve combustion. 1. An internal combustion engine fuel composition comprising:at least one liquid fuel; andat least one gaseous fuel, the gaseous fuel having an effective solubility in the liquid fuel at twenty degrees Celsius and one atmosphere in the range of 0.0000001 g/kg to 0.0002 g/kg, wherein dispersion of the gaseous fuel within the liquid fuel before introduction of the fuel composition to an internal combustion engine is such that molecules of the liquid and gaseous fuels are substantially equidistant one from another, liquid from liquid and gas from gas, within a variance of no more than one hundred percent (±100%),whereby the fuel composition is substantially homogeneous before being introduced to the internal combustion engine such that upon injection the rapid expansion of the gaseous fuel dispersed within the liquid fuel promotes the atomization of the liquid fuel and thus improves combustion, andwherein the time between mixture of the gaseous fuel into the liquid fuel to form the fuel composition and introduction of the fuel composition into the internal combustion engine is at least ...

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Номер записи: 99

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: 100