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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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Форма поиска

Поддерживает ввод нескольких поисковых фраз (по одной на строку). При поиске обеспечивает поддержку морфологии русского и английского языка
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Применить Всего найдено 2963. Отображено 100.
27-09-2012 дата публикации

Methanol to olefins process

Номер: US20120240615A1
Автор: Stephen De Haan
Принадлежит: Lummus Technology Inc

A process for chilling ethylene to required storage temperatures is disclosed, the process including: cooling an ethylene product from at least one of an ethylene production process and an ethylene recovery process via indirect heat exchange with a coolant at a temperature less than about −100° C. to decrease the temperature of the ethylene product; mixing a portion of the cooled ethylene product with methane to form the coolant; expanding at least one of the coolant, the methane, and the portion of the cooled ethylene to reduce a temperature of the coolant to less than −100° C. prior to the cooling; and feeding the heat exchanged coolant to at least one of the ethylene production process, the ethylene recovery process, and an open-loop refrigeration system.

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Номер записи: 1
30-01-2014 дата публикации

Process for the production of aromatic hydrocarbons

Номер: US20140031598A1
Автор: Glenn Charles Komplin, Kuochen Tsai, Sujata Degaleesan, Vishwanath Subramaniam
Принадлежит: Individual

A process comprising feeding bromine into a first reactor; feeding low molecular weight alkanes into the first reactor; and withdrawing alkyl bromides from the first reactor wherein the bromine and low molecular weight alkanes are fed through an apparatus that rapidly mixes the bromine and low molecular weight alkanes. A process is disclosed further comprising reacting the alkyl bromides to form aromatic hydrocarbons.

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Номер записи: 2
07-01-2016 дата публикации

Steam methane reformer system and method of performing a steam methane reforming process

Номер: US20160002035A1
Автор: Jonathan Jay Feinstein, Michael P. RALSTON
Принадлежит: Zoneflow Reactor Technologies LLC

An apparatus includes a furnace having at least one bayonet reforming tube. The furnace is adapted to receive a gas including a hydrocarbon and at least one of steam and carbon dioxide via the bayonet reforming tube, heat and catalytically react the gas to form syngas at a first temperature, cool the syngas to a second temperature lower than the first temperature, and eject the syngas from the tube. The furnace has a first effluent stream including flue gas and a second effluent stream including syngas. The apparatus also includes a first heat recovery section adapted to transfer heat from the first effluent stream to a first heat load including one of air, water, and steam, and a second heat recovery section adapted to transfer heat from the second effluent stream to a second heat load.

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Номер записи: 3
07-01-2016 дата публикации

NOZZLE DESIGN FOR IONIC LIQUID CATALYZED ALKYLATION

Номер: US20160002125A1
Автор: Ahmed Moinuddin, CHANG Bong Kyu, Girgis Michael John, Luo Huping, Mohr Donald Henry, Parimi Krishniah, Timken Hye Kyung Cho
Принадлежит: Chevron U.S.A. INC.

Systems for ionic liquid catalyzed hydrocarbon conversion comprise a reactor vessel, a mixing device in fluid communication with the reactor vessel, and at least one circulation loop in fluid communication with the reactor vessel and the mixing device. The mixing device may comprise an upper venturi, at least one feed injection component, and a lower venturi. Such systems may be used for ionic liquid catalyzed alkylation reactions. Processes for ionic liquid catalyzed hydrocarbon conversion are also disclosed. 1. A system for ionic liquid catalyzed hydrocarbon conversion , the system comprising:a reactor vessel having a top; anda mixing device disposed at the top of the reactor vessel, wherein the mixing device comprises:an upper venturi having an axial outlet at the upper venturi distal end, the upper venturi distal end disposed within the reactor vessel,at least one feed injection array disposed within the reactor vessel, each said feed injection array coaxial with the upper venturi, anda lower venturi having an axial inlet at the lower venturi proximal end, the lower venturi proximal end disposed within the reactor vessel, wherein:the lower venturi inlet is spaced radially outward from the upper venturi outlet to define an inter-venturi channel between the upper venturi distal end and the lower venturi proximal end,the lower venturi is coaxial with the upper venturi,the mixing device is configured for projecting a central jet of a first liquid downward from the upper venturi outlet into the lower venturi, andeach said feed injection array is configured for projecting a second liquid toward an axis of the upper venturi.2. (canceled)3. The system according to claim 1 , wherein the lower venturi inlet is disposed at the same elevation or about the same elevation as the upper venturi outlet.4. The system according to claim 1 , wherein:the lower venturi has a lower venturi constriction point,the at least one feed injection array comprises a single feed injection array ...

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Номер записи: 4
02-01-2020 дата публикации

AROMATIZATION PROCESS USING HEAVY AROMATIC CIRCULATION

Номер: US20200002250A1
Автор: Weber Eric P.
Принадлежит: CHEVRON PHILLIPS CHEMICAL COMPANY LP

Disclosed are a catalytic method and system for producing aromatic hydrocarbons from aliphatic hydrocarbons or light naphtha. In an aspect, the process comprises adding a diluent comprising a heavy aromatic hydrocarbon (for example, C-C) to a reactor feedstock comprising aliphatic hydrocarbons (for example, C-C) or light naphtha to form a reactor feed stream, such that the heat capacity of reactor feed stream is higher than the heat capacity of feedstock. The reactor feed stream is heated and contacting with a catalyst under conditions sufficient to aromatize at least a portion of the aliphatic hydrocarbons and form a product stream comprising a primary aromatic hydrocarbon product and a heavy aromatic hydrocarbon product. In an aspect, the diluent can comprise a heavy aromatic hydrocarbon having at least one carbon atom more than the primary aromatic hydrocarbon product. 1. A catalytic hydrocarbon reforming system comprising:a fractionator having an inlet to receive an initial feedstock comprising naphtha and an outlet to discharge a reactor feedstock comprising aliphatic hydrocarbons;a diluent input line for adding a diluent comprising a heavy aromatic hydrocarbon to the reactor feedstock to form a reactant feed stream having a first temperature;at least one furnace capable of heating the reactant feed stream to a second temperature;at least one reactor charged with a catalyst comprising an inorganic support, a Group 8-10 metal, and at least one halide, the reactor having an inlet to receive the reactant feed stream and an outlet to discharge a reactor effluent stream at a third temperature; and a reactor effluent stream leaving the final reactor comprising a primary aromatic hydrocarbon product and a heavy aromatic hydrocarbon product; 'a first return line extending from the separation system to the diluent input line for providing the diluent, the diluent comprising at least a portion of the heavy aromatic hydrocarbon product.', 'a separation system that ...

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Номер записи: 5
03-01-2019 дата публикации

Combined apparatus for the synthesis of urea

Номер: US20190002401A1
Автор: Andrea Scotto, Enrico Rizzi
Принадлежит: Casale SA

Combined apparatus ( 1 ) for the synthesis of urea from ammonia and carbon dioxide, comprising an internal wall ( 3 ) which delimits two coaxial zones ( 4 ) inside the apparatus, operating respectively as reaction ( 4 ) and condensation ( 5 ) zones, and optionally also comprising a stripping zone and/or a scrubber integrated in the same apparatus.

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Номер записи: 6
02-01-2020 дата публикации

Production Processes, Systems, Methods, and Apparatuses

Номер: US20200002621A1
Автор: Osterloh James D., Spitzauer Michael P.
Принадлежит: GPI PATENT HOLDING LLC

The present disclosure provides production processes that can include exposing a carbon-based material to liquid media to form hydrocarbon fuel. Waste to fuel conversion processes as well as waste material processing reactors are provided that can be configured to convert waste to fuel. Heat exchangers, power generation processes and combustion turbine exhaust apparatus are also provided. Fuel generation processes and generation systems are provided. Reaction media conduit systems as well as processes for servicing reactant media pumps coupled to both inlet and outlet conduits containing reactant media, are also provided. 110-. (canceled)11. A fuel generation system comprising:a reactor configured to house a liquid reaction media and receive solid carbon based material;a distillation apparatus coupled to the reactor and configured to receive gaseous hydrocarbon fuel from the reactor; anda combustion turbine coupled to the distillation apparatus and configured to receive distillate portions from the distillation apparatus.12. The system of further comprising a conveyor apparatus associated with reactor claim 11 , the conveyor apparatus configured to convey material to a receiving portion of the apparatus.13. The system of further comprising a heat exchanger coupled to the reactor claim 11 , the heat exchanger configured to heat the liquid reaction media by providing heat from a heat exchanger fluid.14. The system of wherein the heat exchanger is coupled to the combustion turbine.15. The system of wherein at least a portion of the heat exchanger fluid of the heat exchanger circulates within an exhaust apparatus of the combustion turbine.16. The system of wherein the reactor comprises a media circulating conduit configured to circulate the liquid reaction media.17. The system of wherein conduit comprises a fluid pump claim 16 , the conduit further configured to have the fluid pump removed from the conduit while maintaining substantially all the fluid within the conduit ...

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Номер записи: 7
14-01-2016 дата публикации

Methanol to olefins process

Номер: US20160009609A1
Автор: Stephen De Haan
Принадлежит: Lummus Technology Inc

A process for chilling ethylene to required storage temperatures is disclosed, the process including: cooling an ethylene product from at least one of an ethylene production process and an ethylene recovery process via indirect heat exchange with a coolant at a temperature less than about −100° C. to decrease the temperature of the ethylene product; mixing a portion of the cooled ethylene product with methane to form the coolant; expanding at least one of the coolant, the methane, and the portion of the cooled ethylene to reduce a temperature of the coolant to less than −100° C. prior to the cooling; and feeding the heat exchanged coolant to at least one of the ethylene production process, the ethylene recovery process, and an open-loop refrigeration system.

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Номер записи: 8
14-01-2016 дата публикации

CONTINUOUS POLYMERIZATION DEVICE, METHOD FOR PRODUCING POLYMER COMPOSITION, AND INJECTION VALVE

Номер: US20160009831A1
Автор: NISHITANI Akira, Sumida Masakazu, Yamazaki Kazuhiro
Принадлежит: Sumitomo Chemical Company, Limited

A continuous polymerization apparatus uses at least a first reactor and a second reactor (). Each of the reactors () comprises a supply port () and an effluent port (). The supply port () of the first reactor () is connected to supply sources () of a raw material monomer and a polymerization initiator, and the effluent port () thereof is connected to the supply port () of the second reactor () by a connection line (). The connection line () is combined with a replenishing line () through an injection valve () at a combining part. The injection valve () comprises, in a full closure state thereof, a clearance that may cause a fluid comprising at least the raw material monomer to flow from the replenishing line () to the connection line (). 1. A continuous polymerization apparatus at least comprisinga first reactor and a second reactor, whereineach of the reactors comprises a supply port and an effluent port, whereinthe supply port of the first reactor is connected to supply sources of a raw material monomer and a polymerization initiator, whereinthe effluent port of the first reactor is connected to the supply port of the second reactor by a connection line, whereinthe connection line is combined with a replenishing line through an injection valve at a combining part located between the effluent port of the first reactor and the supply port of the second reactor, and whereinthe injection valve in a full closure state thereof comprises a clearance capable of causing a fluid comprising at least the raw material monomer to flow from the replenishing line to the connection line.2. The continuous polymerization apparatus of claim 1 , whereinthe injection valve comprises:a plug;a body comprising a space that accommodates the plug; anda shaft that supports and operates the plug in the space, and whereinin the full closure state, the clearance is formed between an inner wall face of the body and a surface of the plug.3. The continuous polymerization apparatus of claim 1 , ...

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Номер записи: 9
08-01-2015 дата публикации

Cooling between multiple polyolefin polymerization reactors

Номер: US20150011814A1
Автор: Catherine M. Gill, Elizabeth A. Benham, Joel A. Mutchler, Maruti Bhandarkar, Rebecca A. Gonzales, Scott E. Kufeld, Thanh T. Nguyen, Timothy O. Odi
Принадлежит: Chevron Phillips Chemical Co LP

A system and method for a first reactor to produce a transfer slurry having a first polyolefin polymerized in the first reactor, a heat-removal zone to remove heat from the transfer slurry, and a second reactor to receive the transfer slurry cooled by the heat-removal zone, the second reactor to produce a product slurry having a product polyolefin which includes the first polyolefin and a second polyolefin polymerized in the second reactor.

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Номер записи: 10
09-01-2020 дата публикации

METHODS FOR PREPARATION OF CHA ZEOLITE AT AMBIENT PRESSURE

Номер: US20200010332A1
Автор: Lang David Ari
Принадлежит:

The disclosure, in one aspect, relates to methods of preparing a CHA zeolite under ambient pressure conditions. In further aspects, the disclosure relates to methods such that a mother liquor can be isolated from a disclosed method, and recycled for use in a disclosed method for further preparation of a CHA zeolite. This abstract is intended as a scanning tool for purposes of searching in the particular art and is not intended to be limiting of the present disclosure. 1. A method for preparing a CHA zeolite , the method comprising:heating a zeolite precursor mixture at ambient pressure in a reflux reaction vessel of a reflux reactor system comprising the reflux reaction vessel and a reflux condenser;wherein the zeolite precursor mixture comprises water, a silicate solution, a zeolite, and a CHA templating agent;wherein heating comprises heating the reaction vessel such the zeolite precursor mixture in the reflux reaction vessel has a reaction temperature of from about 80° C. to about 120° C.;thereby forming a CHA zeolite and a mother liquor solution.2. The method of claim 1 , wherein the ambient pressure is about 700 torr to about 800 torr.3. The method of claim 1 , wherein the zeolite in the zeolite precursor mixture is selected from a USY zeolite claim 1 , a pre-treated Na-Y zeolite claim 1 , a Na-Y zeolite claim 1 , and combinations thereof.4. The method of claim 3 , wherein the zeolite in the zeolite precursor mixture is selected from a pre-treated Na-Y zeolite claim 3 , a Na-Y zeolite claim 3 , and combinations thereof.5. The method of claim 3 , wherein the zeolite in the zeolite precursor mixture is a USY zeolite.6. The method of claim 1 , wherein the silicate in the zeolite precursor mixture is a sodium silicate solution comprising SiO claim 1 , NaO claim 1 , and water.7. The method of claim 1 , wherein the CHA templating agent is selected from N claim 1 ,N claim 1 ,N-trimethyl-1-ammonium adamantine claim 1 , tetraethylenepentamine claim 1 , and a combination ...

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Номер записи: 11
21-01-2016 дата публикации

PORTABLE ON-DEMAND SULFUROUS ACID GENERATOR

Номер: US20160016795A1
Автор: GONZALEZ ALEXIS DANIEL
Принадлежит:

Some embodiments of the present disclosure include a portable sulfurous acid generator for producing sulfurous acid on-demand for, for example, a small-scale irrigation system. The sulfurous acid generator may include a hopper for storing an amount of elemental sulfur, a supply chute or auger for transporting the sulfur from the hopper to a burn chamber, wherein the burn chamber is configured to burn the elemental sulfur, producing sulfur dioxide fumes, a Venturi system operatively connected to the burn chamber, the Venturi system configured to transport the fumes from the burn chamber into a holding tank comprising a fluid, creating a sulfurous acid solution, and a pump configured to recirculate the fluid in the system. A user may dispense sulfurous acid from the holding tank into an irrigation system using a dispensing valve, and the sulfurous acid generator may be mounted on a support platform for portability.

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Номер записи: 12
26-01-2017 дата публикации

Continuous reaction apparatus and method of continuous polymerization using the same

Номер: US20170022300A1
Автор: Kazuhiro Hirahara, Takanobu Takeda, Tetsuo Shimizu
Принадлежит: Horiba Stec Co Ltd

The present invention includes a first raw material feeding unit, a second raw material feeding unit, a reactor unit, and a controller configured to control the amount of a first raw material being fed from the first raw material feeding unit to the reactor unit, the amount of a second raw material being fed from the second raw material feeding unit to the reactor unit, the temperature of the first raw material being fed from the first raw material feeding unit to the reactor unit, and the temperature of the second raw material being fed from the second raw material feeding unit to the reactor unit. The first raw material is raw material monomer solution containing a raw material monomer. The second raw material is polymerization initiator solution containing a polymerization initiator. A reaction product is polymer compound resulting from a living anionic polymerization reaction of the raw material monomer.

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Номер записи: 13
10-02-2022 дата публикации

Polymerization of Propylene

Номер: US20220041769A1
Автор: GARNER Bryan M., PARKER Anthony O.
Принадлежит:

Disclosed are a method and system for propylene polymerization utilizing a loop slurry reactor. The method can include polymerizing propylene in a loop slurry reactor under bulk polymerization conditions to produce polypropylene. The propylene polymerization system can include i) a loop slurry reactor and a heat exchange system that is configured to cool the legs of the loop slurry reactor and/or ii) an inlet manifold that is configured to connect flashline heaters to a separator. 1. A method of polymerizing propylene in a loop slurry reactor under bulk polymerization conditions to produce polypropylene , comprising:cooling a plurality of vertical legs of the loop slurry reactor with a coolant flowing at a coolant flow rate;cooling the coolant in a heat exchanger positioned externally of the loop slurry reactor so as to control a temperature difference between a first temperature of the coolant entering the heat exchanger and a second temperature of the coolant exiting the heat exchanger, wherein the heat exchanger has a coolant contact surface;producing polypropylene in the loop slurry reactor at a production rate in a range of from about 75 tons/hr to about 90 tons/hr;{'sup': '3', 'wherein a first ratio of the production rate to the coolant flow rate is in a range of from about 1:40 to about 1:65 tons/hr:m/hr.'}2. The method of wherein a second ratio of the production rate to the temperature difference is in a range of from about 11:1 to about 20:1 tons/hr:° C.3. The method of wherein a third ratio of the production rate to a surface area of the coolant contact surface is in a range of from about 0.0352:1 to about 0.637:1 tons/hr:m.4. The method of wherein a fourth ratio of the production rate to the coolant flow rate to the temperature difference is in a range of from about 1:40:0.087 tons/hr:m/hr:° C. to about 1:65:0.050 tons/hr:m/hr:° C.5. A method of polymerizing propylene in a loop slurry reactor under bulk polymerization conditions to produce polypropylene ...

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Номер записи: 14
24-04-2014 дата публикации

High rate reactor system

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

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

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Номер записи: 15
17-02-2022 дата публикации

METHOD FOR PRODUCING HYDROGEN AND GENERATING ELECTRICAL POWER

Номер: US20220052364A1
Автор: KRATSCHMAR Kenneth William, Leboe David Aaron, Reid Christopher Edwin John, Schubak Gary Edward
Принадлежит:

There is described a method for producing hydrogen and generating electrical power. A hydrocarbon fuel source is decomposed into hydrogen and carbon using a hydrocarbon dissociation reactor. The carbon is separated from the hydrogen in a carbon separator. Electrical power is generated from the separated carbon using a direct carbon fuel cell. 1. A method for producing hydrogen and generating electrical power , comprising:decomposing a hydrocarbon fuel source into hydrogen and carbon using a hydrocarbon dissociation reactor;separating the carbon from the hydrogen in a carbon separator; andgenerating electrical power from the separated carbon using a direct carbon fuel cell (DCFC).2. The method of claim 1 , further comprising purifying the separated hydrogen using a hydrogen separator.3. The method of or claim 1 , further comprising:mixing, in the carbon separator, the separated carbon with a molten carbonate electrolyte to form a slurry,{'claim-text': ['circulating the slurry to the DCFC, wherein in the DCFC at least some carbon comprised in the slurry is converted to carbon dioxide and electrical power, thereby forming a carbon-depleted slurry; and', 'circulating the carbon-depleted slurry away from the DCFC.'], '#text': 'wherein generating electrical power from the separated carbon comprises:'}4. The method of claim 3 , wherein circulating the slurry to the DCFC comprises circulating the slurry to an anode and to an electrolyte flow field of the DCFC claim 3 , and wherein in the anode at least some carbon comprised in the slurry is converted to carbon dioxide and electrical power claim 3 , thereby forming the carbon-depleted slurry.5. The method of claim 3 , wherein circulating the slurry to the DCFC comprises circulating the slurry to an anode of the DCFC and not to an electrolyte flow field of the DCFC claim 3 , and wherein in the anode at least some carbon comprised in the slurry is converted to carbon dioxide and electrical power claim 3 , thereby forming the ...

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Номер записи: 16
11-02-2016 дата публикации

DIRECT COMBUSTION HEATING

Номер: US20160039677A1
Автор: Noyes Dallas B.
Принадлежит: Seerstone LLC

An electrode includes a network of compressed interconnected nanostructured carbon particles such as carbon nanotubes. Some nanostructured carbon particles of the network are in electrical contact with adjacent nanostructured carbon particles. Electrodes may be used in various devices, such as capacitors, electric arc furnaces, batteries, etc. A method of producing an electrode includes confining a mass of nanostructured carbon particles and densifying the confined mass of nanostructured carbon particles to form a cohesive body with sufficient contacts between adjacent nanostructured carbon particles to provide an electrical path between at least two remote points of the cohesive body. The electrodes may be sintered to induce covalent bonding between the nanostructured carbon particles at contact points to further enhance the mechanical and electrical properties of the electrodes. 1. A method , comprising:mixing oxygen with a reducing gas in a vessel having an interior temperature above a reaction temperature of the reducing gas with oxygen;reacting at least a portion of the oxygen with at least a portion of the reducing gas to form at least one carbon oxide in a heated reaction gas mixture; andreacting the heated reaction gas mixture in the presence of a catalyst to form a tail gas and at least one of a solid carbon product and a hydrocarbon.2. The method of claim 1 , wherein mixing oxygen with a reducing gas comprises mixing the oxygen with the reducing gas in a vessel having an interior temperature above about 400° C.3. The method of claim 1 , wherein reacting at least a portion of the oxygen with at least a portion of the reducing gas comprises reacting at least a portion of the oxygen with at least a portion of the reducing gas in the presence of a catalyst selected to promote the exothermic reaction of the at least a portion of the oxygen with at least a portion of the reducing gas to form at least one carbon oxide in a heated reaction gas mixture.4. The ...

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Номер записи: 17
08-02-2018 дата публикации

Portable fuel synthesizer

Номер: US20180036709A1
Автор: Kevin Martin Henson, Roy Alvin Bynum
Принадлежит: Portable Gtl Systems LLC

A portable fuel synthesizer, comprising multiple shipping containers, the various modules within one of the multiple shipping containers, a boiler utilizing a hydrocarbon gas as fuel, a cooling system module connected to the boiler, the cooling system adjusts a temperature of the boiler, a syngas reformer, a reactor connected to the syngas reformer and the boiler, the reactor converts the syngas to a hydrocarbon liquid, a hot separator connected to the reactor, a cold separator connected to the hot separator separates liquid hydrocarbons and gaseous hydrocarbons at a lower temperature and pressure than the hot separator, a distillation unit connected to the cold separator performs fractional distillation and separation of hydrocarbon products received from the cold separator, a recycle module connected to the cold separator and distillation unit recycles unreacted gases to the reactor, and a fuel testing and blending unit to receive separated hydrocarbons from the distillation unit.

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Номер записи: 18
11-02-2016 дата публикации

APPARATUS FOR PRODUCING WATER-ABSORBENT RESIN

Номер: US20160039950A1
Автор: Kotake Masato, KUZUKAWA Masahiro, Nakamura Kenji
Принадлежит: Sumitomo Seika Chemicals Co., Ltd.

In an apparatus for producing the water-absorbent resin, gas heated by the polymerization heat accompanied by a polymerization reaction in a reactor main body flows through a first pipe into a heat exchanging structure, and a cooled fluid obtained by the cooling flows through a second pipe into the reactor main body. In the apparatus, a first pipe temperature adjusting portion adjusts a temperature of the first pipe to fall within a predetermined temperature range, and a polymerization reactor temperature adjusting portion adjusts a temperature of an upper portion of the reactor main body to fall within a predetermined temperature range. 1. An apparatus for producing a water-absorbent resin , comprising: a reactor main body in which the water soluble ethylenically unsaturated monomer and the liquid medium is contained and an upper portion of which is left for a gaseous phase portion, and', 'a gas discharging portion which is connected to the reactor main body and discharges gas of the gaseous phase portion from the reactor main body;, 'a polymerization reactor in which a water-absorbent resin is produced by polymerization reaction on a water soluble ethylenically unsaturated monomer in a liquid medium, the polymerization reactor including'}a first channel portion having a first channel which is connected to the gas discharging portion and through which the gas discharged from the reactor main body by the gas discharging portion flows;a first channel portion temperature adjusting portion which adjusts a temperature of the first channel portion to fall within a predetermined temperature range in which the gas flowing through the first channel of the first channel portion is not condensed; a cooler main body which is connected to the first channel portion, into which the gas flowing through the first channel of the first channel portion flows, and which cools inflow gas, and', 'a cooled fluid discharging portion which is connected to the cooler main body and discharges ...

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Номер записи: 19
18-02-2016 дата публикации

Process and Apparatus for Making Phenol and/or Cyclohexanone

Номер: US20160046550A1
Автор: Becker Christopher L., Coleman John S., Davis Jason D., Nair Hari, Patel Bryan A.
Принадлежит:

A process for producing phenol and/or cyclohexanone by cleaving cyclohexylbenzene hydroperoxide in a loop cleavage reactor comprising multiple reaction zones connected in series. In desirable embodiments, fresh cyclohexylbenzene hydroperoxide feed(s) are supplied to reaction zones the final reaction zone, and fresh acid catalyst is supplied only to the final reaction zone. In desirable embodiments, a portion of the effluent exiting the final reaction zone is recycled to the first reaction zone. Each reaction zone is equipped with a heat exchanger downstream of the feed port to extract heat generated from the cleavage reaction. 1. A process for making phenol and/or cyclohexanone , the process comprising:(A) providing a cleavage reactor having a plurality of reaction zones connected in series, the reaction zones comprising a first reaction zone, a final reaction zone and optionally one or more intermediate reaction zone(s) between the first reaction zone and the final reaction zone; wherein:each of the reaction zones comprises a processed feed port, a fresh feed port, a heat exchanger at least partly downstream of the processed feed port and the fresh feed port in the same reaction zone, and an effluent port, except that the heat exchanger for the final reaction zone is optional;the effluent port of any given reaction zone other than the final reaction zone is in fluid communication with the processed feed port of the immediately following reaction zone in the series; andthe effluent port of the final reaction zone is in fluid communication with the processed feed port of the first reaction zone;(B) supplying a fresh reaction feed comprising cyclohexylbenzene hydroperoxide to each reaction zone other than the final reaction zone via the fresh feed port of the reaction zone and producing an effluent at the effluent port of the reaction zone;(C) supplying at least a portion of the effluent exiting the effluent port of each of the reaction zones other than the final ...

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Номер записи: 20
16-02-2017 дата публикации

REACTORS AND METHODS FOR PRODUCING SOLID CARBON MATERIALS

Номер: US20170043310A1
Автор: Noyes Dallas B.
Принадлежит: Seerstone LLC

A reactor for producing a solid carbon material comprising at least one reaction chamber configured to produce a solid carbon material and water vapor through a reduction reaction between at least one carbon oxide and at least one gaseous reducing material in the presence of at least one catalyst material. Additional reactors, and related methods of producing a solid carbon material, and of forming a reactor for producing a solid carbon material are also described. 1. A reactor for producing a solid carbon material , comprising:at least one reaction chamber configured to produce a solid carbon material and water vapor through a reduction reaction between at least one carbon oxide and at least one gaseous reducing material in the presence of at least one catalyst material structure comprising a catalyst material at least partially extending through the at least one reaction chamber;at least one cooling chamber operatively communicating with the at least one reaction chamber and configured to condense the water vapor produced in the at least one reaction chamber; andat least one conveying mechanism configured to transport the at least one catalyst material structure through the at least one reaction chamber.2. The reactor of claim 1 , wherein the at least one reaction chamber is configured to produce the solid carbon material through at least one of a Bosch reaction claim 1 , a Boudouard reaction claim 1 , and a methane reduction reaction.3. The reactor of claim 1 , wherein the at least one reaction chamber is configured to withstand an operating temperature greater than or equal to about 450° C.4. (canceled)5. The reactor of claim 1 , wherein the at least one cooling chamber is configured to have an operating temperature of less than or equal to about 50° C.6. The reactor of claim 1 , further comprising a heat exchange zone operatively associated with each of at least one effluent gas line and at least one return gas line extending between the at least one reaction ...

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Номер записи: 21
16-02-2017 дата публикации

Process for the preparation of silylated polymers employing a backmixing step

Номер: US20170044303A1
Автор: Brendan O'keefe, Bruce Barbera, John Banevicius, Misty Huang, VIKRAM Kumar
Принадлежит: Momentive Performance Materials Inc

A continuous process for preparing a silylated polymer comprising a silylation step where a prepolymer having reactive functional groups, a first intermediate product, is reacted continuously with a silylating agent in an endcapping tubular reaction unit to form a second intermediate product, and where at least a portion of the second intermediate product is backmixed continuously with the first intermediate product to form the silylated polymer. The continuous process may further comprise a stabilization step, a quenching step or both a stabilization step and a quenching step.

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Номер записи: 22
15-02-2018 дата публикации

PROCESS FOR THE PREPARATION OF SILYLATED POLYMERS EMPLOYING A BACKMIXING STEP

Номер: US20180044466A1
Автор: "OKeefe Brendan", Banevicius John, Barbera Bruce, Huang Misty, Kumar Vikram
Принадлежит:

A continuous process for preparing a silylated polymer comprising a silylation step where a prepolymer having reactive functional groups, a first intermediate product, is reacted continuously with a silylating agent in an endcapping tubular reaction unit to form a second intermediate product, and where at least a portion of the second intermediate product is backmixed continuously with the first intermediate product to form the silylated polymer. The continuous process may further comprise a stabilization step, a quenching step or both a stabilization step and a quenching step. 125-. (canceled)27. The silylated polyurethane of having a color of less than 50 Pt-Co.28. The silylated polyurethane of having less than about 0.02 weight percent isocyanate.35. A process for the preparation of the silylated polymer comprising(a) continuously reacting a prepolymer with a silylating agent, by a silylation reaction, to produce a silylated polymer composition;(b) continuously backmixing at least a first portion of the silylated polymer composition with a loop connected from a downstream outlet to an upstream outlet of a reactor to adjust to at least one upstream process parameter; and{'claim-ref': {'@idref': 'CLM-00026', 'claim 26'}, '(c) continuously reacting at least a second portion of the silylated polymer composition with a cyclic amide scavenging agent or scavenging package containing at least one cyclic amide scavenging agent to produce the quenched silylated polymer of .'}36. The process of claim 35 , wherein the cyclic amide scavenging agent is selected from the group consisting of ε-caprolactam and 2-pyrrolidone.38. The process of claim 44 , wherein the prepolymer is at least one prepolymer selected from the group consisting of a chain extended polyol with terminal hydroxyl groups claim 44 , chain extended polyol with terminal isocyanate groups or a chain extended polyol with both hydroxyl and isocyanate groups39. The process of further comprising adding a ...

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Номер записи: 23
18-02-2016 дата публикации

HYDROGEN GENERATING DEVICE AND POWER GENERATING EQUIPMENT

Номер: US20160049675A1
Автор: CHEN Ying-Chieh, Lin Yu-Hsiang, WANG CHUNG-PING
Принадлежит:

A hydrogen generating device includes a first housing, a porous structure, a first flow-guiding structure and a heating unit. The first housing accommodates a solid reactant. The porous structure is disposed in the first housing. The first flow-guiding structure has first and second end portions opposite to each other. The first end portion is connected to the porous structure. The second end portion protrudes outside the first housing and is connected to the heating unit. A liquid reactant passing through the second end portion is gasified into a gaseous reactant through the heating unit. The gaseous reactant passing through the first end portion reaches to the porous structure and then is diffused from the porous structure into the first housing, so that the gaseous reactant and the solid reactant react and generate a hydrogen gas. A power generating equipment including the hydrogen generating device is also provided. 1. A hydrogen generating device , comprising:a first housing accommodating a solid reactant;a porous structure disposed in the first housing;a first flow-guiding structure having a first end portion and a second end portion opposite to the first end portion, wherein the first end portion is connected to the porous structure, and the second end portion protrudes outside the first housing; anda heating unit connected to the second end portion, wherein a liquid reactant is adapted to be gasified to become a gaseous reactant through the heating unit, and the gaseous reactant passes through the first flow-guiding structure to reach to the porous structure and then is diffused from the porous structure into the first housing, so that the gaseous reactant and the solid reactant react and generate a hydrogen gas.2. The hydrogen generating device as claimed in claim 1 , wherein when a temperature of the porous structure is lower than a temperature value and the gaseous reactant reaches to the porous structure claim 1 , the gaseous reactant is cooled and ...

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Номер записи: 24
21-02-2019 дата публикации

METHOD AND SYSTEM FOR RAPIDLY PREPARING LITHIUM CARBONATE OR CONCENTRATED BRINE USING HIGH-TEMPERATURE STEAM

Номер: US20190055134A1
Автор: PENG Fuming, YU Hao, Zeng Xiong, ZHU Binyuan
Принадлежит:

A method and system for rapidly preparing lithium carbonate or concentrated brine using high-temperature steam. The method comprises the steps of: feeding brine into a reactor, heating the brine with high-temperature steam above 200° C. while simultaneously discharging steam produced in the reactor, cooling and condensing the discharged steam in a condenser and collecting the condensate, and stopping the high-temperature steam after the brine is concentrated to a predetermined concentration or after a sufficient amount of lithium carbonate is collected. The system comprises: a reactor provided with a brine inlet, a steam outlet connected to a condenser, a product outlet, and a plurality of steam pipes. The method concerns the direct heating of brine using high-temperature steam, which is effective and efficient, and also produces fresh water. The heating is uniform and rapid, and does not require jackets, heat exchange tubes, mixers and vacuum pumps, vastly simplifying the system. 1. A method for rapidly preparing lithium carbonate or concentrated brine using high-temperature steam comprising the following steps of:1) feeding brine into a reactor;2) introducing high-temperature steam with a temperature above 200° C. into the brine and heating the brine, while concurrently discharging steam produced in the reactor;3) cooling the discharged steam using a condenser, and collecting the condensate;4) stopping the introduction of the high-temperature steam after the brine is concentrated to a predetermined concentration or after a sufficient amount of lithium carbonate is separated out.2. The method according to claim 1 , wherein the high-temperature steam is introduced into the brine after the brine is preheated to a temperature of not less than 50° C.3. The method according to claim 1 , wherein the high-temperature steam is superheated steam.4. The method according to claim 1 , wherein the temperature of the high-temperature steam is not less than 250° C.5. The method ...

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Номер записи: 25
04-03-2021 дата публикации

METHOD OF PREPARING AROMATIC VINYL COMPOUND-VINYL CYANIDE COMPOUND POLYMER AND APPARATUS FOR PREPARING THE SAME

Номер: US20210061928A1
Автор: HWANG Jeong A, JANG Sungkeun, JOO Eun Jung, LEE Won Kyun, SHIN DAEYOUNG
Принадлежит:

A method of preparing an aromatic vinyl compound-vinyl cyanide compound polymer includes polymerizing a reaction mixture containing an aromatic vinyl compound, a vinyl cyanide compound, and an organic solvent in a reactor and transferring the vaporized reaction mixture present in the upper space of the reactor to a heat exchanger via a pipe and condensing the vaporized reaction mixture. The condensed reaction mixture is transferred to one side of the pipe and sprayed into the pipe, the flow velocity of the reaction mixture vaporized in the reactor is reduced, and temperature is lowered. Accordingly, a phenomenon wherein polymer particles in a reactor are sucked into a heat exchanger is prevented, and occurrence of polymerization in the heat exchanger is suppressed. Therefore, productivity and quality may be improved. 1. A method of preparing an aromatic vinyl compound-vinyl cyanide compound polymer , comprising:polymerizing a reaction mixture containing an aromatic vinyl compound, a vinyl cyanide compound, and an organic solvent in a reactor; andtransferring the vaporized reaction mixture present in an upper space of the reactor to a heat exchanger via a pipe and condensing the vaporized reaction mixture,wherein the condensed reaction mixture is transferred to one side of the pipe and sprayed into the pipe.2. The method according to claim 1 , wherein the spraying is performed so that a flow of the condensed reaction mixture is countercurrent to a flow of the vaporized reaction mixture.3. The method according to claim 1 , wherein the reaction mixture contains 40 to 80% by weight of the aromatic vinyl compound claim 1 , 10 to 35% by weight of the vinyl cyanide compound claim 1 , and 5 to 35% by weight of the organic solvent.4. The method according to claim 1 , wherein the spray comprises all or a portion of the reaction mixture transferred to the heat exchanger.5. The method according to claim 1 , wherein a temperature of the reaction mixture transferred to the heat ...

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Номер записи: 26
05-03-2020 дата публикации

Design of an Ethylene Oligomerization/Trimerization/Tetramerization Reactor

Номер: US20200071243A1
Автор: KREISCHER Bruce E.
Принадлежит:

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 into 5 in, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr)(gal) to 6.0 (lb)(hr)(gal). 1. A process comprising:periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system;oligomerizing the olefin monomer within the reaction mixture to form an oligomer product; andperiodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system;wherein the reaction system comprises: a total reaction mixture volume within the reaction system; and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect thermal contact between the reaction mixture and a heat exchange medium;{'sup': −1', '−1', '−1', '−1, 'wherein an oligomer product discharge rate from the reaction system is between 1.5 (lb)(hr)(gal) to 6.0 (lb)(hr)(gal); and'}{'sup': −1', '−1, 'wherein a ratio of the total heat exchanged surface area ...

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Номер записи: 27
18-03-2021 дата публикации

OLIGOMERISATION METHOD USING A REACTION DEVICE COMPRISING A DISPERSION MEANS

Номер: US20210077977A1
Автор: AUGIER Frederic, Raynal Ludovic, VONNER Alexandre
Принадлежит: IFP ENERGIES NOUVELLES

The present invention relates to an oligomerization process using a reaction device comprising a dispersion means. In particular, the process relates to the oligomerization of ethylene to give linear α-olefins, such as 1-butene, 1-hexene or 1-octene, or a mixture of linear alpha-olefins. 2. The device as claimed in claim 1 , wherein the means for dispersing the cooled liquid fraction is selected from a distributor network claim 1 , a perforated plate or a perforated distributor claim 1 , having an open fraction of between 0.5% and 40%.3. The device as claimed in claim 1 , wherein the means for dispersing the cooled liquid fraction is selected from a packing having a large surface area with respect to the volume thereof and also a small pressure drop claim 1 , preferably the ratio of the surface area with respect to the volume is between 40 and 2500 m/m.4. An oligomerization process employing a device as claimed in claim 1 , said process is carried out at a pressure between 0.1 and 10 MPa claim 1 , at a temperature between 30° C. and 200° C. claim 1 , comprising the following steps:a) a step of introducing the catalytic oligomerization system comprising a metal catalyst and an activating agent into a reaction chamber comprising a liquid phase and a gas phase,b) a step of bringing said catalytic system into contact with ethylene by introducing said ethylene into the lower part of the reaction chamber,c) a step of withdrawing a liquid fraction,d) a step of cooling the liquid fraction drawn off in step c) by passing said liquid fraction into a heat exchanger,e) a step of introducing the liquid fraction cooled in step d) at the top of the reaction chamber,f) a step of dispersing the liquid fraction introduced in step e) in the gas phase in the upper part of the reaction chamber,wherein steps c) to e) constitute a recirculation loop.5. The process as claimed in claim 4 , carried out in a device comprising a reaction chamber comprising a liquid phase and a gas phase claim ...

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Номер записи: 28
19-03-2015 дата публикации

Low Emissions Oxidative Dehydrogenation Process for Producing Butadiene

Номер: US20150080627A1
Автор: Elizabeth BALLARD, Joseph G. Duff, Liana Caciula, Mark J. Potter, Sirisha CHADA
Принадлежит: TPC Group LLC

Butadiene is formed by dehydrogenation of butenes which are mixed with steam and oxygen then converted to butadiene by oxidative dehydrogenation over a ferritic oxide catalyst, wherein the sensible heat in the oxidative dehydrogenation reaction product is utilized along with heat produced by thermal oxidation of low value volatile products formed to reduce energy requirements and CO 2 emissions. Sensible heat is utilized at high temperature for purposes of superheating feed and at somewhat lower temperatures for purposes of vaporizing feed at sequential locations in the process.

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Номер записи: 29
22-03-2018 дата публикации

INTEGRATED PROPANE DEHYDROGENATION PROCESS

Номер: US20180079699A1
Автор: Panditrao Sunil Shashikant, Ram Sanjeev
Принадлежит: LUMMUS TECHNOLOGY INC.

Processes and systems for the integrated production of propylene and an alkylate, such as cumene, may include feeding a hydrocarbon feedstock containing propane to a propane dehydrogenation reaction zone to convert a portion of the propane to propylene. The propylene is separated in a separation system to form a polymer-grade propylene stream, a low purity propylene stream, and a propane stream. The low purity propylene stream is then fed to an alkylation reaction zone where the propylene is reacted to produce an alkylated product and generate a low pressure steam. The low pressure steam may then be fed to the separation system as a heat source, integrating the dehydrogenation system and the alkylation system. 1. A process for the production of cumene comprising:feeding a hydrocarbon feedstock comprising propane to a propane dehydrogenation reaction zone, converting a portion of the propane to propylene, forming a dehydrogenated effluent;separating the dehydrogenated effluent in a separation system, forming a polymer-grade propylene stream, a low purity propylene stream, and a propane stream;feeding the low purity propylene stream to an alkylation reaction zone, wherein propylene is reacted with benzene to concurrently produce an alkylated product and generate a low pressure steam stream; andfeeding the low pressure steam stream to the separating step as a heat source.2. The process of claim 1 , further comprising recycling the propane stream to the propane dehydrogenation reaction zone.3. The process of claim 1 , further comprising separating the alkylated product into one or more of a benzene stream claim 1 , a C3 stream claim 1 , a cumene product stream claim 1 , and a heavies effluent claim 1 , wherein the C3 stream comprises one or more of propane and propylene.4. The process of claim 3 , wherein the separating comprises recovering the C3 stream at a higher pressure than an operating pressure of the propane dehydrogenation reaction zone.5. The process of claim ...

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Номер записи: 30
30-03-2017 дата публикации

Catalyst and Its Use in Dehydrocyclization Processes

Номер: US20170087540A1
Автор: John S. Buchanan, Mayank Shekhar, Paul F. Keusenkothen, Samia ILIAS
Принадлежит: ExxonMobil Chemical Patents Inc

The invention relates to catalysts and their use in processes for dehydrocyclization of light paraffinic hydrocarbon feedstock to higher-value hydrocarbon, such as aromatic hydrocarbon, to dehydrocyclization catalysts useful in such processes, and to the methods of making such catalysts. One of more of the dehydrocyclization catalysts comprising a crystalline aluminosilicate zeolite having a constraint index of less than or equal to about 12, at least one Group 3 to Group 13 metal of the IUPAC Periodic Table and phosphorous.

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Номер записи: 31
30-03-2017 дата публикации

Aromatization of Non-Aromatic Hydrocarbon

Номер: US20170088484A1
Автор: Denton Robert D., Keusenkothen Paul F., Maher David W., Valencia Jaime A.
Принадлежит:

The invention relates to producing aromatic hydrocarbon by aromatization of non-aromatic hydrocarbon, including feed pretreatment, aromatization of the aromatization feed's Chydrocarbon and C non-aromatic hydrocarbon, and recovery of an aromatic product. The invention also relates to modules for carrying out the pretreatment, aromatization, and recovery, and also modules for auxiliary function such as power generation. 1. A system for producing aromatic hydrocarbon , comprising:{'sup': '3', 'sub': 2', '3+', '2+', '3+', '2, "(a) a an aromatizer configured for (i) receiving a preselected amount ≧1 million standard cubic feet per day [MSCFD] (29,000 NMD) of an aromatization feed, the aromatization feed comprising Chydrocarbon and C non-aromatic hydrocarbon and having a preselected C non-aromatic hydrocarbon concentration in the range of from 15 mole % to 90 mole % per mole of aromatization feed, and (ii) aromatization of (A) at least a portion of the aromatization feed's C non-aromatic hydrocarbon and (B) at least a portion of the aromatization feed's Chydrocarbon to produce a reaction effluent comprising molecular hydrogen, non-aromatic hydrocarbon, and aromatic hydrocarbon; and"}(b) a product recoverer in fluidic communication with the aromatizer, the product recoverer being configured for recovering at least first and second products from the reaction effluent, wherein the first product comprises at least a portion of the reaction effluent's aromatic hydrocarbon and the second product comprises a tail gas containing (i) at least a portion of the reaction effluent's molecular hydrogen and (ii) at least a portion of the reaction effluent's non-aromatic hydrocarbon.2. The system of claim 1 , wherein the system further comprises a feed pretreater configured for (A) receiving ≧2 MSCFD (57 claim 1 ,000 NMD) of a gaseous feed and (B) producing the aromatization feed from the gaseous feed claim 1 , the gaseous feed comprising 0 mole % to 98 mole % methane claim 1 , 1 mole % ...

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Номер записи: 32
23-04-2015 дата публикации

Method and apparatus for manufacturing graphite oxide

Номер: US20150108400A1
Автор: Byoung Kyu Ji, Cheol Min Shin, Jung Young Choi, Shi Choon Lee
Принадлежит: IDT International Co Ltd

There is provided a method and an apparatus for preparing graphite oxide, in accordance with the present disclosure, when an oxidizer is added by stages into a sequencing batch oxidizer mixer connected in multiple stages at a constantly low temperature, the oxidizer is mixed therein while suppressing an oxidation reaction. During an oxidation reaction of graphite, in a risky range of overheating and explosion, a tube type reactor equipped within a heat exchanger is used to accurately control a local temperature and the oxidizer can permeate between layers of the graphite with increased efficiency under ultrasonication. In an additional reaction range out of the risky range, a continuous stirred tank reactor is used to mature the oxidation reaction, so that a risk of explosion during manufacturing of graphite oxide can be reduced and a great amount of graphite oxide can be mass-produced economically.

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Номер записи: 33
27-04-2017 дата публикации

PROCESS FOR HEAVY OIL UPGRADING IN A DOUBLE-WALL REACTOR

Номер: US20170114286A1
Автор: Alabdulhadi Abdullah T., Choi Ki-Hyouk, LEE Joo-Hyeong
Принадлежит:

A process for reducing coke formation during hydrocarbon upgrading reactions using a double-wall reactor comprising the steps of feeding a heated feed water to a shell-side volume of the double-wall reactor to produce a heat transfer stream, the double-wall reactor comprising an exterior wall and an interior wall, a reaction section volume, a heating element configured to heat the heat transfer stream, wherein heat is transferred from the heat transfer stream to the reaction section volume, feeding the hot water return exiting the shell-side volume through a filter; mixing the filtered water stream with a heated hydrocarbon feedstock; feeding the mixed stream to the reaction section volume in a configuration counter-current to the heat transfer stream; reacting the reaction flow stream at a reaction temperature, wherein the heat transferred to the reaction section volume is operable to maintain the reaction temperature above the critical temperature of water. 1. A supercritical water plant to upgrade hydrocarbons with reduced coke formation , the supercritical water plant comprising:a hydrocarbon feedstock pump, the hydrocarbon feedstock pump configured to pressurize a hydrocarbon feedstock to a pressure above the critical pressure of water to produce a pressurized hydrocarbon feedstock;a hydrocarbon feedstock heater fluidly connected to the hydrocarbon feedstock pump, the hydrocarbon feedstock heater configured to heat the pressurized hydrocarbon feedstock to a temperature greater than 50° C. to produce a heated hydrocarbon feedstock;a feed water pump, the feed water pump configured to pressurize a feed water to a pressure above the critical pressure of water to produce a pressurized feed water;a feed water heater fluidly connected to the feed water pump, the feed water pump configured to heat the pressurized feed water to a temperature above the critical temperature of water to produce a heated feed water;a double-wall reactor, the double-wall reactor configured ...

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Номер записи: 34
26-04-2018 дата публикации

Reformer With Bypass For Internal Fuel Cell Reforming

Номер: US20180115002A1
Автор: Eric Dean, Michael Jennings, Robert Cunningham
Принадлежит: LG FUEL CELL SYSTEMS INC

A fuel cell system having a fuel cell stack, comprising an anode portion and a cathode portion, a source of hydrocarbon fuel, and a reformer unit having one or more cold-side, reforming passages, a fuel supply conduit, a reformate exhaust conduit, one or more hot-side channels, a cathode exhaust conduit, a cathode inlet conduit, one or more bypass channels having non-reforming passages for fuel to bypass the cold-side channels, and a flow controller for controlling the flowrate in the bypass channels, and methods for operating the same, is provided.

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Номер записи: 35
07-05-2015 дата публикации

Multi-phase reactor system with slinger liquid reflux distributor

Номер: US20150126771A1
Автор: Rajaram S. Ghadge, Thomas Mathew
Принадлежит: Reliance Industries Ltd

A multi-phase reactor system for performing multi-phase reactions is disclosed. The reactor system includes a reaction vessel having a slinger device ( 100 ) mounted on a centrally positioned agitator shaft ( 102 ) proximal to an operative top of the reaction vessel. The slinger device ( 100 ) comprises a holding means defined by a vertical circumferential plate ( 108 ) and a cover plate ( 107 ) for at least partially encasing the agitator shaft ( 102 ) to define a space for collecting a liquid. The holding means comprise at least one spraying means including spray pipes ( 106 ) for distributing the liquid on an inner wall of the reaction vessel by a projectile trajectory path on rotation of the agitator shaft. A concave blade ( 104 ) may be positioned over the cover plate ( 107 ) for preventing overflow of the liquid from the holding means and forming an umbrella of the flowing liquid to effect scrubbing of the vapors and off-gas.

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Номер записи: 36
24-07-2014 дата публикации

Reactor liquid cooldown method

Номер: US20140202204A1
Автор: Jeff HARRINGTON
Принадлежит: Air Liquide Large Industries US LP

A reactor liquid cool down method is provided. The method includes obtaining a warm recycle stream ( 102 ) from a reactor ( 101 ) and compressing the warm recycle stream ( 102 ), thereby producing a compressed warm recycle stream ( 104 ); mixing a compressed warm recycle stream ( 104 ) with a controlled liquid cryogen stream ( 110 ) in a stainless steel mixing zone ( 107 ), thereby producing a cool recycle stream ( 112 ), wherein the cool recycle stream has a mean fluid temperature, monitoring the mean fluid temperature and comparing the mean fluid temperature to a predetermined control valve set point, thereby defining a temperature deviation; modulating a temperature control valve ( 109 ) to vary the controlled liquid cryogen stream ( 110 ) in order to produce a temperature deviation that is less than a predetermined value, and returning the cool recycle stream ( 112 ) to the reactor ( 101 ).

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Номер записи: 37
04-05-2017 дата публикации

PROCESS FOR THE PREPARATION OF AN ETHYLENE COPOLYMER IN A TUBULAR REACTOR

Номер: US20170121434A1
Автор: Slots Sjors, Van Bodegom Robert, Van Kan Joannes Augustinus Maria
Принадлежит:

The invention relates to a process a system and a high pressure pump for the preparation of a copolymer of ethylene and a di- or higher functional (meth) acrylate in a tubular reactor, comprising the steps of: injecting ethylene at a pressure of 100 MPa to 350 MPa into the reactor from a high pressure compressor and injecting the (meth)acrylate at a pressure of 100 MPa to 350 MPa into the reactor from a high pressure pump, wherein the high pressure pump comprises—a pump suction chamber for receiving a medium to be compressed; —a cylinder for receiving the medium to be compressed from the pump suction chamber; —an outlet for discharging a compressed medium from the cylinder, —a seal fixed to the inner wall of the cylinder at an end of the cylinder distal to the outlet and —a plunger movable in the cylinder by sliding through the seal, wherein a leakage gap is present along the plunger and the leakage gap is fluidly connected to the pump suction chamber. 2. The process according to claim 1 , wherein the (meth)acrylate is cooled before entering the high pressure pump.3. The process according to claim 1 , wherein the meth(acrylate) is fed to the high pressure pump at a temperature of at most 10° C.4. The process according to claim 1 , wherein the seal is made of PTFE.5. The process according to claim 1 , wherein the meth(acrylate) is fed to the high pressure pump from a feed passage provided with a cooling unit supplied with chilled water.6. The process according to claim 1 , wherein the high pressure pump is cooled by a flushing oil cooler claim 1 , wherein the flushing oil cooler is supplied with chilled water.7. The process according to claim 5 , wherein the cooling unit and the flushing oil cooler are supplied with chilled water from a single chilled water unit.8. The process according to claim 1 , wherein the copolymerisation takes place at a peak temperature between 290° C. and 350° C.9. The process according to claim 1 , wherein the (meth)acrylate is applied in ...

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Номер записи: 38
27-05-2021 дата публикации

Design of an Ethylene Oligomerization/Trimerization/Tetramerization Reactor

Номер: US20210155562A1
Автор: KREISCHER Bruce E.
Принадлежит:

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 into 5 in, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr)(gal) to 6.0 (lb)(hr)(gal). 1. A reaction system for oligomerizing an olefin monomer , the reaction system comprising:one or more reaction system inlets configured to periodically or continuously introduce an olefin monomer, a catalyst system or catalyst system components, or any combination thereof to a reaction mixture within the reaction system;one or more reaction system reaction mixture outlets configured to periodically or continuously discharge a reaction system effluent comprising an oligomer product from the reaction system;a total reaction mixture volume within the reaction system; anda heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect thermal contact between the reaction mixture and a heat exchange medium;wherein an oligomer product discharge rate from the reaction system is between 1.5 lb/hr/gal to 6.0 lb/hr/gal; and{'sup': −1', '−1, 'wherein a ratio of the total heat exchanged surface area to the total ...

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Номер записи: 39
21-05-2015 дата публикации

Liquid fuel cpox reformers and methods of cpox reforming

Номер: US20150137044A1
Автор: Caine M. Finnerty, Paul DEWALD
Принадлежит: WATT Fuel Cell Corp

A liquid fuel catalytic partial oxidation (CPOX) reformer can include a plurality or an array of spaced-apart CPOX reactor units, each reactor unit including an elongate tube having a gas-permeable wall with internal and external surfaces, the wall enclosing an open gaseous flow passageway with at least a portion of the wall having CPOX catalyst disposed therein and/or comprising its structure. The catalyst-containing wall structure and open gaseous flow passageway enclosed thereby define a gaseous phase CPOX reaction zone, the catalyst-containing wall section being gas-permeable to allow gaseous CPOX reaction mixture to diffuse therein and hydrogen rich product reformate to diffuse therefrom. At least the exterior surface of the CPOX reaction zone can include a hydrogen barrier. The liquid fuel CPOX reformer can include a vaporizer, one or more igniters, and a source of liquid reformable fuel.

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Номер записи: 40
10-05-2018 дата публикации

PROCESSES AND SYSTEMS FOR CONTROLLING COOLING FLUID IN AN IONIC LIQUID REACTOR SYSTEM WITH A HEAT EXCHANGER

Номер: US20180128560A1
Автор: Hagen James G., Mueller Sean G., Pham Trung, Schrad Gregory J., Xu Zhanping
Принадлежит:

Processes for controlling the rate and temperature of cooling fluid through a heat exchange zone in, for example, an alkylation reactor using an ionic liquid catalyst. A cooling fluid system may be used to provide the cooling fluid which includes a chiller and a reservoir. The cooling fluid may pass from the reservoir through the heat exchange zone. A bypass line may be used to pass a portion of the cooling fluid around the heat exchange zone. The amount of cooling fluid may be adjusted, with a valve, based upon the temperature of the cooled process fluid flowing out of the heat exchange zone. Some of the cooling fluid from the chiller may be circulated back to the chiller in a chiller loop. 1. A process for controlling a flow of a cooling fluid through a heat exchanger , the process comprising:passing a cooling fluid from a chilling zone to a reservoir;passing a first portion of the cooling fluid from the reservoir through a heat exchange zone;passing a second portion of the cooling fluid from the reservoir through a bypass line around the heat exchange zone;passing a process fluid through the heat exchange zone; and,absorbing heat from the process fluid with the cooling fluid in the heat exchange zone to provide a cooled process fluid.2. The process of for comprising: adjusting the second portion of the cooling fluid from the reservoir that flows through a bypass line based upon a temperature of the cooled process fluid.3. The process of wherein a temperature of the first portion of the cooling fluid from the reservoir is between approximately −6.7 to 26.7° C. (20 to 80° F.).4. The process of wherein a temperature of the first portion of the cooling fluid from the reservoir is between approximately 1.7 to 12.8° C. (35 to 55° F.).5. The process of wherein the heat exchange zone comprises a plurality of heat exchangers.6. The process of wherein a first heat exchanger from the plurality of heat exchangers receives a process fluid from a first reaction zone claim 5 , ...

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Номер записи: 41
19-05-2016 дата публикации

DEGASSING SYSTEM AND DEVICE FOR DEGASSING LIQUID SULFER

Номер: US20160137499A1
Автор: Forbes Brandon W., Groves Brian Nathaniel Greenway, Willingham Thomas C.
Принадлежит:

Embodiments of the invention are directed to a sulfur recovery system that utilizes a degassing system for degassing liquid sulfur. The degassing system includes a degassing device vessel, a pressure equalizer, a motive force device, a sulfur cooler, and/or a process gas cooler. The degassing system may be located within or outside of the sulfur recovery unit and utilizes the process gas from the sulfur recovery unit. The degassing device may receive liquid sulfur and process gas, which are passed through a catalyst, which along with the process gas, degasses the liquid sulfur. As such, the degassing system when used within the sulfur recovery unit degasses the liquid sulfur to reduce off-gassing of dangerous hydrogen sulfide during storage and transportation without the need for additional equipment to degas the liquid sulfur during or after the sulfur storage. 1. A degassing system for a sulfur recovery system , comprising:a degassing vessel, wherein the degassing vessel is configured to receive liquid sulfur from one or more condensers and process gas from any location of the sulfur recovery system, wherein the degassing vessel outputs degassed liquid sulfur for storage, and wherein the degassing vessel returns the process gas used to degas the liquid sulfur to the sulfur recovery system at any location; anda downstream pressure equalizer, wherein the downstream pressure equalizer receives the degassed liquid sulfur from the degassing vessel, separates the degassed liquid sulfur from any remaining gas, and delivers the degassed liquid sulfur to sulfur storage without the remaining gas.2. The degassing system of claim 1 , further comprising:a motive force device configured to supplement pressure of the process gas exiting the degassing vessel and being returned to the sulfur recovery system.3. The degassing system of claim 1 , further comprising:{'sub': '2', 'at least one sulfur cooler configured to receive the liquid sulfur from the one or more condensers, cool ...

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Номер записи: 42
26-05-2016 дата публикации

APPARATUS AND PROCESS FOR TREATING NATURAL GAS

Номер: US20160144335A1
Автор: Catchpole Stephen John
Принадлежит: JOHNSON MATTHEY PLC

A process is described for treating a natural gas stream containing methane and one or more higher hydrocarbons including the steps of mixing at least a portion of the natural gas stream with steam; passing the mixture adiabatically over a supported precious metal reforming catalyst to generate a reformed gas mixture comprising methane, steam, carbon dioxide, carbon monoxide and hydrogen; cooling the reformed gas mixture to below the dew point to condense water and removing the condensate to provide a de-watered reformed gas mixture, and passing the de-watered reformed gas mixture through an acid gas recovery unit to remove carbon dioxide and at least a portion of the hydrogen and carbon monoxide, thereby generating a methane stream. The methane stream may be used to adjust the composition of a natural gas stream, including a vapourised LNG stream, to meet pipeline specifications. 1. An apparatus for treating a natural gas stream containing methane and one or more higher hydrocarbons comprising:(i) means for adding steam and hydrogen to a natural gas stream,(ii) a reformer vessel operatively connected to the means for adding steam and hydrogen, said reformer vessel containing a supported precious metal reforming catalyst, configured such that the natural gas stream and steam are passed over the catalyst to generate a reformed gas mixture comprising methane, steam, carbon dioxide, carbon monoxide and hydrogen,(iii) heat exchange means operatively connected to the reformer vessel to cool the reformed gas mixture to below the dew point and separation equipment operatively connected to the heat exchange means to recover process condensate and provide a de-watered reformed gas mixture, and(iv) an acid gas recovery unit operatively connected to the separation equipment to remove carbon dioxide and at least a portion of the hydrogen and carbon monoxide, thereby generating a methane stream.2. The apparatus according to further comprising a natural gas liquefaction unit ...

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Номер записи: 43
09-05-2019 дата публикации

SYSTEMS AND METHODS FOR PRODUCTION AND SEPARATION OF HYDROGEN AND CARBON DIOXIDE

Номер: US20190135626A1
Автор: Allam Rodney John, Rafati Mohammad
Принадлежит:

The present disclosure relates to systems and methods useful for providing one or more chemical compounds in a substantially pure form. In particular, the systems and methods can be configured for separation of carbon dioxide from a process stream, such as a process stream in a hydrogen production system. As such, the present disclosure can provide systems and method for production of hydrogen and/or carbon dioxide. 1. A process for separating carbon dioxide (CO) from a process stream comprising COand one or more further components , the process comprising:{'sub': '2', 'providing the process stream at a pressure such that a partial pressure of the COin the process stream is at least 15 bar;'}{'sub': '2', 'drying the process stream sufficiently so that a dew point of the process stream comprising the COis reduced to a temperature of about −20° C. or less;'}{'sub': '2', 'cooling the process stream in at least one heat exchanger to provide the process stream comprising the COas a two phase stream;'}expanding the two phase stream so as to reduce the temperature of the two phase stream to a temperature that is within about 15° C. of a freezing point of the two phase stream; and{'sub': '2', 'separating the two phase stream to provide a vapor stream enriched with at least one of the one or more further components and to provide a liquid stream that is enriched with the CO.'}2. The process of claim 1 , wherein the drying comprises passage of the process stream comprising the COthrough a desiccant-packed bed.3. The process of claim 1 , wherein the cooling comprises cooling the process stream against at least a portion of the liquid stream that is enriched with the CO.4. The process of claim 3 , wherein the cooling comprises cooling the process stream in a first heat exchanger and in a second heat exchanger.5. The process of claim 4 , wherein the cooling comprises cooling the process stream in the first heat exchanger against a first portion of the liquid stream that is ...

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Номер записи: 44
30-04-2020 дата публикации

REACTOR LAYOUT FOR METHANOL PRODUCTION FROM LOW QUALITY SYNTHESIS GAS

Номер: US20200131105A1
Автор: Modarresi Hassan
Принадлежит:

A reactor layout for a process of methanol production from low quality synthesis gas, in which relatively smaller adiabatic reactors can be operated more efficiently, some of the inherent disadvantages of adiabatic reactors for methanol production are avoided. This is done by controlling the outlet temperature in the pre-converter by rapid adjustment of the recycle gas, i.e. by manipulating the gas hourly space velocity in the pre-converter. 1. A reactor layout for carrying out the process for methanol production from synthesis gas , said reactor layout comprising:one or more methanol pre-converters/guard reactors, in which the synthesis gas is partially converted to methanol over a heterogeneous catalyst to generate an effluent gas without impurities,a feed-effluent heat exchanger for cooling the effluent gas from the one or more methanol pre-converters/guard reactors, and a main methanol converter for converting a mixture of recycle gas and the cooled effluent gas from the one or more methanol pre-converters/guard reactors,', 'a main feed-effluent heat exchanger,', 'a cooler or a series of coolers,', 'a high pressure gas-liquid separator, which splits the inlet flow into raw methanol and recycle gas,', 'a recycle compressor, and', 'a loop purge., 'a methanol synthesis loop comprising2. The reactor layout according to claim 1 , said reactor layout further comprising means for defining and controlling a maximum allowable outlet temperature using a cold recycle gas stream which is injected into the one or more pre-converters/guard reactors via a control valve.3. The reactor layout according to claim 1 , which has fresh feed gas splitting located on the cold side claim 1 , before the feed-effluent heat exchanger.4. The reactor layout according to claim 1 , which enables on-stream catalyst replacement in the one or more pre-converters/guard reactors. This is a divisional of application Ser. No. 15/749,607, filed on Feb. 1, 2018, which is a 371 of PCT/EP2016/066877, ...

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Номер записи: 45
24-05-2018 дата публикации

LIQUID FUEL REFORMER INCLUDING A VAPORIZER AND METHOD OF REFORMING LIQUID REFORMABLE FUEL

Номер: US20180141807A1
Автор: Dewald Paul, Finnerty Caine M.
Принадлежит:

A liquid fuel reformer includes a fuel vaporizer which utilizes heat from an upstream source of heat, specifically, an electric heater, operable in the start-up mode of the reformer, and therefore independent of the reforming reaction zone of the reformer, to vaporize fuel in a downstream vaporization zone. 118-. (canceled)19. A method of reforming a liquid reformable fuel , the method comprising:introducing an oxygen-containing gas into a conduit for routing fluids toward an inlet of a reformer;heating a stream of the oxygen-containing gas with at least one of a first source of heat comprising an electric heater disposed in the conduit and a second source of heat disposed in the conduit comprising heat of exotherm from the liquid fuel reformer and/or a hydrogen reformate-consuming device external to the liquid fuel reformer to provide a stream of heated oxygen-containing gas;introducing into the stream of heated oxygen-containing gas through or proximate to a vaporizer a liquid reformable fuel to provide a heated gaseous reforming reaction mixture; andreforming the heated gaseous reforming reaction mixture to produce a hydrogen-rich reformate.20. The method of claim 19 , comprising:heating the stream of the oxygen-containing gas and/or the stream of heated oxygen-containing gas with a third source of heat comprising an electric heater disposed in the conduit downstream from the first and second sources of heat and upstream from the vaporizer.21. The method of claim 20 , comprising:discontinuing heating the stream of oxygen-containing gas with the first source of heat; andheating the stream of oxygen-containing gas with the second and third sources of heat.22. The method of comprising adjusting the heat supplied by the second source and/or third source of heat.23. The method of claim 19 , comprising heating the liquid reformable fuel using the second source of heat and/or the third source of heat claim 19 , when present claim 19 , prior to introducing the liquid ...

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Номер записи: 46
17-06-2021 дата публикации

Polymerization of Propylene

Номер: US20210179746A1
Автор: GARNER Bryan M., PARKER Anthony O.
Принадлежит:

Disclosed are a method and system for propylene polymerization utilizing a loop slurry reactor. The method can include polymerizing propylene in a loop slurry reactor under bulk polymerization conditions to produce polypropylene. The propylene polymerization system can include i) a loop slurry reactor and a heat exchange system that is configured to cool the legs of the loop slurry reactor and/or ii) an inlet manifold that is configured to connect flashline heaters to a separator. 1. A method comprising:polymerizing propylene in a loop slurry reactor under bulk polymerization conditions to produce polypropylene;{'sup': '3', 'wherein a space time yield (STY) for the step of polymerizing is greater than 0.36 and less than 0.60 ton polypropylene/hr/mof the loop slurry reactor.'}2. The method of claim 1 , further comprising:cooling a plurality of vertical legs of the loop slurry reactor with a coolant flowing at a coolant flow rate;cooling the coolant in a heat exchanger positioned externally of the loop slurry reactor so as to control a temperature difference between a first temperature of the coolant entering the heat exchanger and a second temperature of the coolant exiting the heat exchanger, wherein the heat exchanger has a coolant contact surface;producing polypropylene in the loop slurry reactor at a production rate in a range of from about 75 tons/hr to about 90 tons/hr;{'sup': '3', 'wherein a first ratio of the production rate to the coolant flow rate is in a range of from about 1:40 to about 1:65 tons/hr:m/hr;'}wherein a second ratio of the production rate to the temperature difference is in a range of from about 11:1 to about 20:1 tons/hr:° C.;{'sup': '2', 'wherein a third ratio of the production rate to a surface area of the coolant contact surface is in a range of from about 0.0352:1 to about 0.637:1 tons/hr:m; and'}{'sup': 3', '3, 'wherein a fourth ratio of the production rate to the coolant flow rate to the temperature difference is in a range of from ...

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Номер записи: 47
01-06-2017 дата публикации

UNIFIED COOLING FOR MULTIPLE POLYOLEFIN POLYMERIZATION REACTORS

Номер: US20170152328A1
Автор: Curren Joseph, Gupta Anurag, Odi Timothy O., Romig Ralph
Принадлежит: CHEVRON PHILLIPS CHEMICAL COMPANY LP

A system and method for startup of a polyolefin reactor temperature control system having a first reactor temperature control path, a second reactor temperature control path, and a shared temperature control path. In some embodiments, during startup the second reactor temperature control path is configured to allow the temperature of a second reactor to rise due to the heat of the exothermic polymerization reaction occurring within reactor until reaching a predetermined setpoint temperature. In other embodiments, during startup a first reactor temperature control path is configured to include a heat exchanger used as a cooler, and a second reactor temperature control path is configured to include a heat exchanger used as a heater, to raise the temperature of the second reactor until reaching a predetermined setpoint temperature. 1. A method of controlling reactor temperature during startup conditions , comprising:splitting a first control feed system into at least (1) a first heat exchanger zone feed stream through a first heat exchanger zone to produce a first heat exchanger zone output stream and (2) a first heat exchanger zone bypass stream;combining the first heat exchanger zone output stream and the first heat exchanger zone bypass stream to give a first treated stream having a first treated stream temperature;recycling a first return stream comprising the first treated stream after the first treated stream has exchanged energy with a first polyolefin reactor;splitting a second control feed stream into at least (1) a second heat exchanger zone feed stream through a second heat exchanger zone to produce a second heat exchanger zone output stream and (2) a second heat exchanger zone bypass stream;combining the second heat exchanger zone output stream and the second heat exchanger zone bypass stream to give a second treated stream having a second treated stream temperature;recycling a second return stream comprising the second treated stream after the second ...

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Номер записи: 48
09-06-2016 дата публикации

BISPHENOL A PREPARATION APPARATUS AND PREPARATION METHOD

Номер: US20160159716A1
Автор: Kim Tae Woo, Lee Jong Ku, Park Jong Suh, PARK Se Ho, Shin Joon Ho
Принадлежит:

Provided are an apparatus and a method for preparing bisphenol A. In the present invention, all or some of a mother liquid stream is circulated to a flash rector through a bypass line after crystallization in a process of preparing bisphenol A so as to increase a conversion rate of bisphenol A in a reactor, reduce energy, and use a heating source of phenol to be discharged to an upper side of the flash reactor, and thus the reaction efficiency of the whole process can be increased. 1. A bisphenol A preparing apparatus comprising:a main reactor that discharges a reaction product of a reaction between phenol and acetone through a reaction product stream;a flash reactor that separates the reaction product stream into a bisphenol A concentration stream and a phenol concentration stream;a bisphenol A purification unit that separates the bisphenol A concentration stream into a bisphenol A purification stream and a mother liquid stream and discharges the separated mother liquid stream to the main reactor; anda bypass line that introduces at least some of the separated mother liquid stream into the flash reactor.2. The bisphenol A preparing apparatus of claim 1 , further comprising:a heating source that supplies heat to the flash reactor.3. The bisphenol A preparing apparatus of claim 1 , further comprising:a recovery reactor that discharges a recovered reaction product, which is obtained by additionally reacting the mother liquid stream separated in the bisphenol A purification unit, to the main reactor through a recovered reaction product stream,wherein the bypass line is positioned between the recovery reactor and the main reactor.4. The bisphenol A preparing apparatus of claim 1 , further comprising:a dehydrator that is positioned between the main reactor and the flash reactor and separates the reaction product stream into a reactor reflux stream and a bisphenol A production stream.5. The bisphenol A preparing apparatus of claim 1 , wherein the bisphenol A purification ...

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Номер записи: 49
16-06-2016 дата публикации

IONIC LIQUID REACTOR WITH HEAT EXCHANGER

Номер: US20160167012A1
Автор: Daly Phillip F., Detrick Kurt, Hagen James, Victor Sanford A., Xu Zhanping
Принадлежит:

An ionic liquid reactor unit and a process for controlling heat generation from an ionic liquid reactor unit. The ionic liquid reactor unit may include an external heat exchanger. The effluent from the reactor is separated in a separation zone allowing the hydrocarbon phase to transfer heat to a cooling fluid. The heat exchanger may be a tube-in-shell, a spiral plate heat exchanger, a hair pin heat exchanger. The heat exchanger accommodates the separation of the ionic liquid from the hydrocarbon phase, and may allow for the ion liquid to be drained. 1. An ionic liquid catalyst reactor unit comprising:a first reaction zone having an inlet for ionic liquid, an inlet for a hydrocarbon stream, and an outlet for an effluent stream;a separation zone configured to receive the effluent stream and separate the effluent stream into a hydrocarbon phase and an ionic liquid phase; and,a first heat exchange zone configured to receive at least a portion of the effluent stream from the first reaction zone and comprising: an outlet for a cooled effluent stream, and an outlet for ionic liquid.2. The ionic liquid catalyst reactor unit of wherein the first heat exchange zone comprises a heat exchanger with a shell and wherein the separation zone is disposed within the shell.3. The ionic liquid catalyst reactor unit of wherein the shell includes an inlet for the effluent stream disposed below the outlet for the cooled effluent stream.4. The ionic liquid catalyst reactor unit of claim 1 , wherein the first heat exchange zone comprises a heat exchanger comprising a shell and at least one baffle in the shell.5. The ionic liquid catalyst reactor unit of wherein the at least one baffle comprises a baffle selected from the group consisting of: a helical baffle; a rod baffle; a grid baffle; an expanded metal baffle; and claim 4 , a segmental baffle.6. The ionic liquid catalyst reactor unit of wherein the heat exchanger is configured to receive the effluent stream in a direction countercurrent ...

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Номер записи: 50
15-06-2017 дата публикации

Hydrogen Sulfide Production Process and Related Reactor Vessels

Номер: US20170166447A1
Автор: Hasenberg Daniel M, Mertens Ives, Pauwels Alex
Принадлежит:

The present invention discloses a hydrogen sulfide reactor vessel with an external heating system that is conductively and removably attached to an exterior portion of the reactor vessel. Also disclosed are processes for producing hydrogen sulfide utilizing the reactor vessel. 1. A HS reactor vessel comprising:(a) a reaction chamber comprising a reactor wall, the reaction chamber configured to contain liquid sulfur;(b) a reactor inlet for liquid sulfur, the reactor inlet positioned at an upper portion of the reactor vessel;(c) a reactor outlet for liquid sulfur, the reactor outlet positioned at a lower portion of the reactor vessel;(d) a gas inlet for a hydrogen-containing gas, the gas inlet connected to a gas distributor, the gas distributor positioned above the reactor outlet for liquid sulfur and configured to inject the hydrogen-containing gas into the liquid sulfur in the reaction chamber;{'sub': '2', '(e) a gas outlet for a HS-rich gas stream, the gas outlet positioned above the reactor inlet;'}(f) an internal heating system, the internal heating system positioned in the liquid sulfur in the reaction chamber during continuous operation of the reactor vessel and configured to maintain an operating temperature above the melting point of sulfur; and(g) an external heating system comprising a heated reactor conduit conductively and removably attached to a portion of an exterior surface of the reactor wall, wherein at least a portion of the heated reactor conduit is positioned in close proximity to the internal heating system and is configured to maintain a start-up temperature of the liquid sulfur above the melting point of sulfur at least until a level of the liquid sulfur in the reaction chamber is above the internal heating system.2. The vessel of claim 1 , wherein the reactor vessel is configured for an operating temperature of at least about 300° C.3. The vessel of claim 1 , wherein the hydrogen-containing gas comprises H.4. The vessel of claim 1 , wherein ...

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Номер записи: 51
22-06-2017 дата публикации

SYSTEMS FOR PRODUCING SOLID CARBON BY REDUCING CARBON OXIDES

Номер: US20170174517A1
Автор: Noyes Dallas B.
Принадлежит: Seerstone LLC

An apparatus for producing solid carbon and water by reducing carbon oxides with a reducing agent in the presence of a catalyst includes a reactor configured to receive reaction gas comprising at least one carbon oxide, at least one reducing agent, and water. The apparatus includes at least one mixing means configured to mix the reagents to form a combined feed, a first heat exchanger configured to heat the combined feed, at least one heater configured to further heat the combined feed, and a reaction vessel configured to receive the combined feed. The reaction vessel is configured to contain a catalyst, to maintain predetermined reaction conditions of temperature and pressure, and has an output configured to deliver a tail gas to the first heat exchanger. The system also includes a product separator, a water separation unit, and a product packaging unit. 125.-. (canceled)26. An apparatus for producing solid carbon by catalytically reducing carbon oxides using a reducing agent , the apparatus comprising:a gas supply system configured to provide a fresh feed gas of carbon oxide and a mixed fresh feed gas comprising carbon oxide and a reducing agent; at least one air-handling device configured to compress the recycled gas with the mixed fresh feed gas to a predetermined pressure and pass the compressed gas to a surge tank;', 'an output line from the surge tank configured to combine the compressed gas and the first portion of the fresh feed gas of carbon oxide to form a combined feed gas;', 'at least one gas-composition analyzer configured to analyze at least one parameter of the combined feed gas; and', 'a control system feedback loop configured to use the at least one parameter of the combined feed gas to regulate a composition of the combined feed gas;, 'a gas handling system having an input line to receive a recycled gas, the mixed fresh feed gas, and a first portion of the fresh feed gas of carbon oxide, the gas handling system comprising a first heat exchanger ...

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Номер записи: 52
08-07-2021 дата публикации

Production of 1-Butene and Ultra-High-Molecular-Weight Polyethylene

Номер: US20210206890A1
Автор: Al Yami Hussain, Ali Ola S., Melebari Faisal, XU WEI
Принадлежит:

A system and method for producing 1-butene and ultra-high-molecular-weight polyethylene (UHMWPE), including feeding a catalyst, an antifouling co-catalyst, and ethylene to a reactor, and dimerizing ethylene into 1-butene and polymerizing a relatively small portion of the ethylene into UHMWPE. A product slurry including 1-butene and UHMWPE is discharged from reactor and UHMWPE is removed from the product slurry as a coproduct of the product 1-butene. The coproduct UHMWPE may be a byproduct that is a relatively small amount of the product slurry. The quantity of UHMWPE produced may be small in comparison to the quantity of 1-butene produced. 2. The method of claim 1 , comprising adjusting a molar ratio of the AFA co-catalyst to titanium (Ti) fed to the reactor to affect molecular weight of the polyethylene to give the UHMWPE claim 1 , wherein the molecular weight of the polyethylene varies inversely with the molar ratio of the AFA co-catalyst to Ti.3. The method of claim 1 , wherein removing comprises filtering UHMWPE from the effluent as coproduct UHMWPE.4. The method of claim 1 , comprising treating the coproduct UHMWPE with acid to remove metal residues comprising aluminum and titanium from the coproduct UHMWPE.5. The method of claim 1 , comprising pelletizing the coproduct UHMWPE.6. The method of claim 1 , comprising combining an antifouling compound (AFC) and a co-catalyst to give the AFA co-catalyst claim 1 , wherein the co-catalyst comprises an aluminum alkyl claim 1 , and wherein feeding the catalyst comprises feeding the catalyst to the reactor separate from the AFA co-catalyst.7. The method of claim 6 , comprising adjusting a ratio of a molar rate of the AFC combined with the co-catalyst to a molar rate of Ti in the catalyst fed to the reactor to affect molecular weight of the UHMWPE claim 6 , wherein the molecular weight of the UHMWPE varies inversely with the ratio.8. The method of claim 6 , wherein the AFC comprises at least one of a phosphonium claim 6 , ...

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Номер записи: 53
28-06-2018 дата публикации

DEGASSING SYSTEM AND DEVICE FOR DEGASSING LIQUID SULFUR

Номер: US20180179061A1
Автор: Forbes Brandon W., Groves Brian Nathaniel Greenway, Willingham Thomas C.
Принадлежит:

Embodiments of the invention are directed to a sulfur recovery system that utilizes a degassing system for degassing liquid sulfur. The degassing system includes a degassing device vessel, a pressure equalizer, a motive force device, a sulfur cooler, and/or a process gas cooler. The degassing system may be located within or outside of the sulfur recovery unit and utilizes the process gas from the sulfur recovery unit. The degassing device may receive liquid sulfur and process gas, which are passed through a catalyst, which along with the process gas, degases the liquid sulfur. As such, the degassing system when used within the sulfur recovery unit degasses the liquid sulfur to reduce off-gassing of dangerous hydrogen sulfide during storage and transportation without the need for additional equipment to degas the liquid sulfur during or after the sulfur storage. 1. A degassing system for a sulfur recovery system , comprising: a liquid sulfur inlet assembly configured for directing liquid sulfur into the degassing vessel;', 'a degassing gas inlet assembly configured for directing degassing gas into the degassing vessel;', 'a catalyst zone configured for facilitating degassing of the liquid sulfur;', 'a liquid sulfur outlet assembly configured for directing degassed liquid sulfur away from the degassing vessel; and', 'a degassing gas outlet assembly configured for directing the degassing gas away from the degassing vessel., 'a degassing vessel, wherein the degassing vessel comprises2. The degassing system of claim 1 , wherein the catalyst zone further comprises:a plurality of catalyst particles in a packed bed or a structured packing coated with the catalyst material.3. The degassing system of claim 1 , wherein the catalyst zone is structured to facilitate interaction between the liquid sulfur and the degassing gas to degas the liquid sulfur such that HS is extracted from the liquid sulfur and directed away from the degassing vessel through the degassing gas outlet ...

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Номер записи: 54
15-07-2021 дата публикации

METHOD AND SYSTEM FOR POLYMER PRODUCTION

Номер: US20210214470A1
Автор: Blanchard Bradley K., Dhodapkar Shrikant, Ewart Sean W., Haun, Jain Pradeep, JR. George W., JR. Michael J., Pollard Maria, Rubalcaba Jorge, Swindoll Robert D., Wang Alec Y., Zogg
Принадлежит:

Disclosed herein is a system for solution polymerization comprising a reactor system that is operative to receive a monomer and to react the monomer to form a polymer; a plurality of devolatilization vessels located downstream of the reactor system, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel; and a heat exchanger disposed between two devolatilization vessels and in fluid communication with them, where the heat exchanger has an inlet port temperature of 100° C. to 230° C., an outlet port temperature of 200° C. to 300° C., an inlet port pressure of 35 to 250 kgf/cmand an outlet port pressure of 20 to 200 kgf/cm; and wherein the polymer solution remains in a single phase during its residence in the heat exchanger. 1. A system for solution polymerization comprising:a reactor system that is operative to receive at least one monomer in a solvent and to react the monomer to form a polymer;a plurality of devolatilization vessels located downstream of the reactor system, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel and wherein the plurality of devolatilization vessels receives a polymer solution from the reactor system; and{'sup': 2', '2, 'a first heat exchanger disposed between two devolatilization vessels and in fluid communication with them, where the first heat exchanger has an inlet port temperature of 120° C. to 230° C., an outlet port temperature of 200° C. to 300° C., an inlet port pressure of 35 to 250 kgf/cmand an outlet port pressure of 20 to 200 kgf/cm; and wherein the polymer solution remains in a single phase during its residence in the first heat exchanger.'}2. The system of claim 1 , further comprising a distributor disposed in at least one devolatilization vessel claim 1 , wherein the distributor comprises: a second conduit; where the first conduit lies inside the second conduit to define a first annular space therebetween; where the ...

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Номер записи: 55
16-07-2015 дата публикации

Methods and systems for coding synthesis gas

Номер: US20150196885A1
Автор: Anant Pisut, Iwan H. Chan, John Abughazaleh, Yongchao Li
Принадлежит: Kellogg Brown and Root LLC

A heat exchanger including a housing. A plurality of tubes can be disposed within the housing. A plurality of solid particulates can be disposed within the housing between an inner surface of the housing and outer surfaces of the tubes, wherein the solid particulates have an average cross-sectional length from about 250 μm to about 5 mm.

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Номер записи: 56
16-07-2015 дата публикации

PURIFICATION APPARATUS INCLUDING CONTINUOUS REACTORS AND PURIFICATION METHOD USING CONTINUOUS REACTORS

Номер: US20150196890A1
Автор: CHOI Gyeong Rye, HONG Jong Pal, LEE CHIL WON, Lee Hee Wan
Принадлежит:

The present invention relates to a purification apparatus and a purification method using the purification apparatus, which apparatus involves diffusing/agitating a solution stored in a solution storage tank with the ultrasonic wave, transferring the solution to a reactor through an air compressor and then mixing the solution in the reactor with a solvent fed through another passage to produce a reactant. 1. A purification apparatus comprising:a solution storage tank to store a solution;an ultrasonic diffuser to diffuse particles contained in the solution of the solution storage tank with an ultrasonic wave;an agitator to agitate the solution stored in the solution storage tank;a heating jacket provided outside the solution storage tank to control an internal temperature of the solution storage tank;an air compressor to suction and transfer the solution of the solution storage tank to a next position; anda continuous reactor to receive the solution transferred by the air compressor and a solvent transferred through a separate passage, and to agitate the solution at a high speed to continuously produce a reactant having uniform particles.2. A purification apparatus comprising:a solution storage tank to store a solution;an ultrasonic diffuser to diffuse particles contained in the solution of the solution storage tank with an ultrasonic wave;an agitator to agitate the solution stored in the solution storage tank;a heating jacket provided outside the solution storage tank to control an internal temperature of the solution storage tank;an air compressor to suction and transfer the solution of the solution storage tank to a next position;a filter cartridge to filter out minute impurities contained in the solution transferred by the air compressor;a temperature control device comprising a casing to receive the filter cartridge, a thermal fluid filled in the casing, and a heater to heat the thermal fluid;a continuous reactor to receive the solution passing through the ...

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Номер записи: 57
22-07-2021 дата публикации

REACTOR FOR A METALLOCENE CATALYST-BASED SOLUTION POLYMERIZATION PROCESS FOR PREPARING POLYOLEFIN POLYMERS

Номер: US20210220794A1
Автор: KIM Yangkee
Принадлежит:

Disclosed is a reactor for solution polymerization process using a metallocene catalyst for preparing polyolefin. The reactor includes: a reaction vessel for mixing a hydrocarbon-based solvent and an olefin monomer to produce polyolefin; a feed inlet installed at a lower portion of the reaction vessel to feed a feed including an unreacted monomer, a solvent, and a catalyst into the reaction vessel; a guide pipe having a cylinder shape being open at respective ends, installed along a central axis of the reaction vessel, and dividing an internal space of the reaction vessel into an up-flow region where a reaction mixture flows upward and a down-flow region where the reaction mixture flows downward; a swirling flow-inducing blade attached to the exterior surface of the guide pipe, causing the reaction mixture in the reaction vessel to rise along the exterior surface of the guide pipe while forming a swirling flow. 1. A reactor for a solution polymerization process using a metallocene catalyst for preparing polyolefin polymers , the reactor comprising:a reaction vessel configured to mix a hydrocarbon-based solvent and an olefin monomer, thereby preparing polyolefin polymers;a feed inlet installed at a lower portion of the reaction vessel and feeding a feed including an unreacted monomer, a solvent, and a catalyst into the reaction vessel;a guide pipe having a cylinder shape being open at respective ends, installed in the reaction vessel along a central axis of the reaction vessel, and dividing an internal space of the reaction vessel into an up-flow region where a reaction mixture flows upward and a down-flow region where the reaction mixture flows downward;a swirling flow-inducing blade having a helical screw blade shape and attached to an exterior surface of the glide pipe, the swirling flow-inducing blade causing the reaction mixture in the reaction vessel to rise along the exterior surface of the guide pipe while forming a swirling flow, then to enter into the guide ...

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Номер записи: 58
14-07-2016 дата публикации

SYNTHESIS GAS AND NANOCARBON PRODUCTION METHOD AND PRODUCTION SYSTEM

Номер: US20160199807A1
Автор: Nakamura Satoru, Tada Akio
Принадлежит:

A synthesis gas and nanocarbon production method has a lower hydrocarbon decomposition step for decomposing lower hydrocarbon to produce hydrogen and nanocarbon, a carbon dioxide reduction step for reacting a part of the nanocarbon produced with carbon dioxide to produce carbon monoxide, and a mixing step for mixing the hydrogen and carbon monoxide produced in a predetermined ratio, thereby nanocarbon and a synthesis gas having a desired gas ratio can be simultaneously produced easily. 111.-. (canceled)12. A synthesis gas and nanocarbon production system , comprising:a lower hydrocarbon decomposition reactor, in which a lower hydrocarbon supply tube for supplying lower hydrocarbon is connected thereto, a catalyst is stored in a space communicated with the lower hydrocarbon supply tube, and the space is a reaction space where the lower hydrocarbon is directly decomposed;carbon monoxide production reactor, in which a carbon dioxide supply tube for supplying carbon dioxide is connected thereto, nanocarbon is stored in a space communicated with the carbon dioxide supply tube, and the space is a reaction space where the carbon dioxide is reduced to carbon monoxide; anda mixing equipment, which is connected to the lower hydrocarbon decomposition reactor and the carbon monoxide production reactor, and in which the hydrogen produced in the lower hydrocarbon decomposition reactor and the carbon monoxide produced in the carbon monoxide production reactor are mixed.13. The synthesis gas and nanocarbon production system according to claim 12 , further comprising:a heat exchanger for cooling the hydrogen produced in the lower hydrocarbon decomposition reactor; anda waste heat supply tube for supplying heat obtained by the heat exchanger to at least one of the lower hydrocarbon decomposition reactor and the carbon monoxide production reactor.14. The synthesis gas and nanocarbon production system according to claim 12 ,wherein the lower hydrocarbon decomposition reactor and the ...

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Номер записи: 59
14-07-2016 дата публикации

GRAPHENE, METHOD AND APPARATUS FOR PREPARING GRAPHENE

Номер: US20160200581A1
Автор: Do Seung Hoe, Jeon Seong Yun, KONG Jung Ho, Lee Jin Seo
Принадлежит:

There are provided a graphene having an oxygen atom content in a predetermined range or less and a carbon/oxygen weight ratio in a specific range to show excellent electrical and thermal conductivity properties, and a barrier property, and a method and an apparatus for preparing the graphene having excellent electrical and thermal conductivity properties and a barrier property by using a subcritical-state fluid or a supercritical-state fluid. According to the method and the apparatus for preparing the graphene, impurities such as graphene oxide, and the like, may be effectively removed, such that uniformity of the graphene to be prepared may be increased, and therefore, the graphene which is highly applicable as materials throughout the industry may be mass-produced. 1. A graphene having 20 wt % or less of an oxygen content and 5 or more of a carbon/oxygen weight ratio (C/O ratio).2. The graphene of claim 1 , wherein a primary differential curve has a peak at 600 to 850° C. in thermogravimetric analysis (TGA).3. The graphene of claim 1 , wherein a primary differential curve does not have a peak at 100 to 300° C. in thermogravimetric analysis (TGA).4. The graphene of claim 1 , wherein a weight loss rate at 900° C. is 90% or more in thermogravimetric analysis (TGA).5. The graphene of claim 1 , wherein an electrical conductivity is 20 S/cm or more.6. The graphene of claim 1 , wherein it is used as at least one selected from the group consisting of barrier materials claim 1 , lightweight materials claim 1 , energy claim 1 , batteries claim 1 , electronics claim 1 , electrics claim 1 , semiconductors claim 1 , steel claim 1 , displays claim 1 , home electronics claim 1 , mobile phones claim 1 , nano-industries claim 1 , biotechnologies claim 1 , polymer composites claim 1 , metal composites claim 1 , paints claim 1 , pastes claim 1 , inks claim 1 , water treatment claim 1 , waste-water treatment claim 1 , antistatic materials claim 1 , electrostatic dispersion materials ...

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Номер записи: 60
14-07-2016 дата публикации

Forced Gas Recirculation in Later Stage Refining Processes and Reactors

Номер: US20160200987A1
Автор: Appel Brian S., Appel Jonathan, Freiss James H.
Принадлежит:

In later stage hydrocarbon fuel refining processes involving cracking reactions for upgrading hydrocarbon containing feeds into liquid and gaseous hydrocarbon fuels, the ration of liquid to gaseous recovery is advantageously increased by forced recirculation of non-condensing gas into cracking reaction. 1. A method , comprising:providing a hydrocarbon compound containing feed in a reaction vessel;subjecting said feed to a cracking reaction in the reaction vessel;removing vapors produced in the cracking reaction, said vapors removed through a reaction vessel outlet;condensing a condensable fraction of the removed vapors to produce at least one liquid hydrocarbon; andrecycling non-condensing gases from the removed vapors back into the reaction vessel.2. The method of claim 1 , wherein said recycling is at a volumetric flow rate exceeding a normal vapor exit volumetric flow rate claim 1 , the normal vapor exit volumetric flow rate corresponding to the flow rate of vapor through the outlet that would be created by vapor production in the reaction vessel at said reaction conditions absent said recycling.3. (canceled)4. The method of claim 2 , wherein said recycling comprises recycling only non-condensing gases.5. The method of claim 4 , wherein said subjecting said feed to a cracking reaction comprises:heating the feed to temperatures of in the range of approximately 400-600° C.; andcontrolling pressure to be in a range of approximately 0.5 to 70 psig.6. The method claim 1 , wherein said recycling comprises continuously forcing the non-condensing gas back to the reaction vessel during the cracking reaction.7. (canceled)8. The method of claim 6 , further comprising adding a reagent to the recycled non-condensing gas and enhancing reagent interaction in solid claim 6 , liquid and gas phases in the cracking reaction by controlling the pressure at a level above approximately 3 bar.9. (canceled)10. The method of claim 6 , further comprising condensing and removing water from ...

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Номер записи: 61
30-07-2015 дата публикации

Oxidative Coupling of Methane Implementations for Olefin Production

Номер: US20150210610A1
Автор: Cizeron Joel, Duggal Suchia, Harraz Hatem, HONG Jin Ki, Iyer Rahul, McCormick Jarod, Radaelli Guido, Rafique Humera A., Scher Erik C., Vuddagiri Srinivas
Принадлежит:

The present disclosure provides oxidative coupling of methane (OCM) systems for small scale and world scale production of olefins. An OCM system may comprise an OCM subsystem that generates a product stream comprising C compounds and non-C impurities from methane and an oxidizing agent. At least one separations subsystem downstream of, and fluidically coupled to, the OCM subsystem can be used to separate the non-C impurities from the C compounds. A methanation subsystem downstream and fluidically coupled to the OCM subsystem can be used to react Hwith CO and/or COin the non-C impurities to generate methane, which can be recycled to the OCM subsystem. The OCM system can be integrated in a non-OCM system, such as a natural gas liquids system or an existing ethylene cracker. 1. An oxidative coupling of methane (OCM) system , comprising:{'sub': 4', '2+', '2+, '(a) an OCM subsystem that (i) takes as input a feed stream comprising methane (CH) and a feed stream comprising an oxidizing agent, and (ii) generates from said methane and said oxidizing agent a product stream comprising C compounds and non-C impurities; and'} (1) said first heat exchanger cools said product stream,', {'sub': 2+', '2+, '(2) said de-methanizer unit accepts said product stream from said first heat exchanger and generates an overhead stream comprising methane and at least a portion of said non-C impurities, and a bottoms stream comprising at least a portion of said C compounds, and'}, '(3) at least a portion of said overhead stream is cooled in said second heat exchanger and is subsequently directed to said first heat exchanger to cool said product stream., '(b) at least one separations subsystem downstream of, and fluidically coupled to, said OCM subsystem, wherein said separations subsystem comprises a first heat exchanger, a de-methanizer unit downstream of said first heat exchanger, and a second heat exchanger downstream of said de-methanizer unit, wherein'}2. The system of claim 1 , wherein ...

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Номер записи: 62
30-07-2015 дата публикации

METHOD FOR REDUCING ENERGY CONSUMPTION IN A PROCESS TO PRODUCE STYRENE VIA DEHYDROGENATION OF ETHYLBENZENE

Номер: US20150210613A1
Автор: Oleksy Slawomir A.
Принадлежит: Technip Process Technology, Inc.

The present invention is directed to improved methods and systems for increasing the efficiency of a dehydrogenation section of an alkenyl aromatic hydrocarbon production facility, wherein an alkyl aromatic hydrocarbon, such as ethylbenzene, is dehydrogenated to produce an alkenyl aromatic hydrocarbon, such as styrene. The disclosed methods are more energy-efficient and cost effective than currently known methods for manufacturing styrene. The methods and systems advantageously utilize multiple reheat exchangers arranged in a series and/or parallel configuration that result in an energy consumption reduction and, consequently, a utility cost savings, as well as a reduction in styrene manufacturing plant investment costs. 1. A method for increasing the efficiency of a dehydrogenation section of an alkenyl aromatic hydrocarbon production facility , said dehydrogenation section for dehydrogenating alkyl aromatic hydrocarbons to alkenyl aromatic hydrocarbons , said method comprising:providing at least a first and a second dehydrogenation reactor,a feed stream comprising said alkyl aromatic hydrocarbons,wherein the first reactor effluent is heated in two or more reheat exchangers arranged in a series with respect to each other, said two or more reheat exchangers being located between the first and the second reactor, and each reheat exchanger is provided with an independent stream of superheated steam, wherein (a) the steam flow rate of superheated steam to the two or more reheat exchangers is equal to or less than the steam flow rate of superheated steam to a single-reheat exchanger in an equivalent dehydrogenation section for dehydrogenating alkyl aromatic hydrocarbons to alkenyl aromatic hydrocarbons, and (b) the temperature of the superheated steam to the two or more reheat exchangers is equal to or less than the temperature of superheated steam required by the single-reheat exchanger.2. The method of claim 1 , wherein the dehydrogenation section further comprises a ...

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Номер записи: 63
29-07-2021 дата публикации

Supercritical water and ammonia oxidation system and process

Номер: US20210229054A1
Автор: AQIL Jamal, Mourad Younes
Принадлежит: Saudi Arabian Oil Co

The present application provides systems and methods for upgrading an oil stream. The system includes a reactor, a phase separator, an expansion device, a cooling unit, and two separation units. The reactor receives the oil stream, ammonia, and supercritical water. The supercritical water upgrades the oil stream, and the ammonia reacts with sulfur initially present in the oil stream to produce ammonia-sulfur compounds. The phase separator receives a mixture stream comprising the upgraded oil stream, supercritical water, and the ammonia-sulfur compounds, and separates out non-dissolved components. The expansion device reduces the pressure of the mixture stream below a water critical pressure. The cooling unit reduces the temperature of the mixture stream. A first separation unit separates the mixture stream it into a hydrocarbon-rich gaseous phase, a water stream containing ammonia-sulfur compounds, and a treated oil stream. A second separation unit separates the ammonia-sulfur compounds from the water stream.

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Номер записи: 64
06-08-2015 дата публикации

CONVERSION OF TRIACYLGLYCERIDES-CONTAINING OILS

Номер: US20150217265A1
Автор: Greene Marvin I.
Принадлежит:

A process for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels is disclosed. The process may include reacting a triacylglycerides-containing oil-carbon dioxide mixture at a temperature in the range from about 250° C. to about 525° C. and a pressure greater than about 75 bar to convert at least a portion of the triacylglycerides to a hydrocarbon or mixture of hydrocarbons comprising one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics. 132-. (canceled)33. A system for converting triacylglycerides-containing oils into crude oil precursors and/or distillate hydrocarbon fuels , the system comprising:a mixing device for mixing a triacylglycerides-containing oil feed with carbon dioxide to form an oil-CO2 mixture;a thermal reforming reactor for reacting the oil-CO2 mixture at a temperature in the range of 250° C. to about 525° C. and a pressure greater than about 75 bar to produce a reaction effluent; anda separator for separating the reaction effluent into a first separation product comprising carbon dioxide and a second separation product comprising hydrocarbon compounds including one or more of isoolefins, isoparaffins, cycloolefins, cycloparaffins, and aromatics.34. The system of claim 33 , further comprising one or more fluid conduits for recycling the first separation product to at least one of the mixing device to form the oil-CO2 mixture and the thermal reforming reactor to control temperature within the thermal reforming reactor.35. The system of claim 33 , further comprising a hydrotreater to hydrotreat at least a portion of the second separation product.36. The system of claim 33 , further comprising a fractionator for fractionating hydrocarbons in the second separation product to form one or more hydrocarbon fractions boiling in the naphtha claim 33 , jet or diesel range.37. The system of claim 35 , further comprising a fractionator for fractionating hydrocarbons in the ...

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Номер записи: 65
06-08-2015 дата публикации

SYSTEMS AND PROCESSES FOR PRODUCING LIQUID TRANSPORTATION FUELS

Номер: US20150217266A1
Автор: Sherwood Steve
Принадлежит:

Disclosed in the application include systems and processes for producing a liquid transportation fuel product using a carbon-containing feedstock. 1. A system for converting a carbon-containing feedstock into a liquid transportation fuel product , the system comprising{'sub': 2', '2', '2', '2', '2, 'an air-blown producer gas reactor operable to convert the carbon-containing feedstock into a producer gas comprising H, CO, CO, and N, with substoichiometeric amounts of Hand CO (less than 2:1 molar ratio of Hto CO);'} wherein the F-T reactor is fluidly coupled to a source of feed gas and operable to convert at least a portion of the feed gas into a FTS product, wherein the FTS product comprises the liquid transportation fuel product and a first residue, and', 'wherein the cracker is fluidly coupled to the F-T reactor and operable to catalytically crack at least a portion of the first residue to produce an additional amount of the liquid transportation fuel product and a second residue; and, 'a processing unit, wherein the processing unit comprises a Fischer-Tropsch (F-T) reactor, and a cracker,'}a product upgrading unit, wherein the product upgrading unit is operable to produce an additional amount of the liquid transportation fuel product from a product gas.2. The system of claim 1 , wherein the carbon-containing feedstock comprises at least one feedstock selected from the group consisting of a ligno-cellulosic biomass solid claim 1 , a biomass derived oil claim 1 , a biomass derived gas claim 1 , and a fossil-fuel derived carbonaceous feedstock.3. The system of claim 1 , wherein the F-T reactor is fluidly coupled to the air-blown producer gas reactor claim 1 , wherein the feed gas to the F-T reactor comprises the producer gas.4. The system of claim 1 , wherein the product gas comprises at least a portion of the first residue or at least a portion of the second residue.5. The system of comprising a hard-wax trap claim 1 , wherein the hard-wax trap is fluidly coupled to ...

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Номер записи: 66
27-07-2017 дата публикации

ALKYLATION SYSTEM AND A PROCESS FOR COOLING A VENT STREAM

Номер: US20170209807A1
Автор: Mehlberg Robert L.
Принадлежит:

One exemplary embodiment can be a process for cooling a vent stream from a receiver. Generally, the process may include providing a refrigerant including at least one compound contained in the receiver so the refrigerant leaking into the receiver can be compatible with the process. 1. A process for cooling a vent stream from a receiver of a depropanizer column in an acid alkylation unit , comprising providing a refrigerant comprising a propane to one or more cooling coils contained in a vent condenser of the receiver wherein the propane in the one or more cooling coils is at a pressure greater than the receiver.2. The process according to claim 1 , wherein the refrigerant in the one or more cooling coils is at a temperature of no more than about −30° C.3. The process according to claim 1 , wherein the receiver is at a pressure of no more than about 1 claim 1 ,720 kPa.4. The process according to claim 1 , further comprising sending the refrigerant contained in the one or more cooling coils to a pump. This application is a Division of copending application Ser. No. 14/597,776 filed Jan. 15, 2015, which application is a Division of application Ser. No. 12/493,662 filed Jun. 29, 2009, now U.S. Pat. No. 8,937,208, the contents of which cited applications are hereby incorporated by reference in their entirety.This invention generally relates to an alkylation system, and a process for cooling a vent stream from a receiver of a depropanizer column in the system.Often a fractionation zone is positioned downstream of an acid alkylation unit to separate the hydrocarbons into various streams and any remaining acid. In the fractionation zone, often one or more columns are utilized for providing these separate streams. Usually, the first column in the series receiving the alkylation zone effluent provides an overhead stream that can include light hydrocarbons and the acid. Often, the acid can be recycled back to the alkylation unit.In the receiver of the first column, a chiller ...

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Номер записи: 67
03-08-2017 дата публикации

Low Emissions Oxidative Dehydrogenation Apparatus for Producing Butadiene

Номер: US20170216811A1
Автор: Ballard Elizabeth, Caciula Liana, Chada Sirisha, Duff Joseph G., Potter Mark J.
Принадлежит:

An apparatus for producing butadiene by way of oxidative dehydrogenation of a butane-rich feed stream includes: (a) a reactor adapted for receiving said butane-rich feed stream and converting butenes to butadiene by oxidative dehydrogenation, thereby providing a butadiene enriched product effluent stream which exits the reactor at an elevated temperature; (b) a superheater coupled to the reactor to receive the butadiene enriched product effluent stream from the reactor at elevated temperature as well as being configured to receive reactor feed, said superheater being adapted to transfer sensible heat from the butadiene enriched product effluent stream to reactor feed and provide superheated feed to the reactor and (c) a first feed vaporizer coupled to the superheater to receive the butadiene enriched product effluent stream as it exits the superheater and to transfer sensible heat from the butadiene enriched product effluent stream to reactor feed. Also provided are (d) a second feed vaporizer coupled to the reactor for providing vapor feed thereto; (e) a purification train for recovering butadiene from the butadiene enriched product effluent stream; and (f) a thermal oxidizer for recovering energy by way of oxidizing by-products from the purification train and providing energy for said second vaporizer. 1. An apparatus for producing butadiene by way of oxidative dehydrogenation of a butane-rich feed stream comprising:(a) a reactor adapted for receiving said butane-rich feed stream and converting butenes to butadiene by oxidative dehydrogenation, thereby providing a butadiene enriched product effluent stream which exits the reactor at an elevated temperature;(b) a superheater coupled to the reactor to receive the butadiene enriched product effluent stream from the reactor at elevated temperature as well as being configured to receive reactor feed, said superheater being adapted to transfer sensible heat from the butadiene enriched product effluent stream to reactor ...

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Номер записи: 68
02-07-2020 дата публикации

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Номер: US20200207685A1
Автор: Cizeron Joel, Czerpak Peter, Faz Carlos, McCormick Jarod, Michalak William, Nyce Greg, Patel Bipinkumar, Radaelli Guido, Rappold Tim A., Runnebaum Ron, Scher Erik C., Zhang Aihua
Принадлежит:

Integrated systems are provided for the production of higher hydrocarbon compositions, for example liquid hydrocarbon compositions, from methane using an oxidative coupling of methane system to convert methane to ethylene, followed by conversion of ethylene to selectable higher hydrocarbon products. Integrated systems and processes are provided that process methane through to these higher hydrocarbon products. 120.-. (canceled)21. A method of producing a plurality of hydrocarbon products including hydrocarbon compounds with two or more carbon atoms (C compounds) , comprising:{'sub': '2+', '(a) directing methane and an oxidant to an oxidative coupling of methane (OCM) reactor that is upstream of a post-bed cracking (PBC) unit, wherein the OCM reactor is configured to facilitate an OCM reaction using the methane and the oxidant to generate the C compounds including ethylene and one or more alkanes, and wherein the PBC unit is configured to convert the one or more alkanes, including ethane, to one or more alkenes, including ethylene;'}(b) in the OCM reactor, reacting the methane and the oxidant in the OCM reaction to generate an OCM product stream and heat, wherein the OCM product stream comprises ethylene and one or more alkanes;(c) directing the OCM product stream to the PBC unit;(d) in the PBC unit, subjecting the OCM product stream to thermal cracking under conditions that crack ethane to ethylene, wherein the thermal cracking is conducted at least in part with the heat from (b), thereby producing a PBC product stream comprising ethylene;(e) directing the PBC product stream to a separations module, and, in the separations module, separating ethane from the PBC product stream to generate an ethane stream; and(f) directing the ethane stream to the PBC unit.22. The method according to claim 21 , wherein the PBC unit is a section of the OCM reactor.23. The method according to claim 21 , wherein the PBC unit is separate from the OCM reactor.24. The method according to ...

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Номер записи: 69
11-08-2016 дата публикации

CHEMICAL-LIQUID MIXING METHOD AND CHEMICAL-LIQUID MIXING APPARATUS

Номер: US20160228832A1
Автор: Hiroshiro Koukichi, KAMIMURA Fumihiro, Tanaka Hiroshi
Принадлежит: TOKYO ELECTRON LIMITED

The present invention provides a chemical-liquid mixing method and a chemical-liquid mixing apparatus capable of sufficiently generating a peroxomonosulfuric acid that is effective in removing a resist from a substrate, when a sulfuric acid and a hydrogen peroxide solution are mixed with each other. At first, an inner tank is filled up with a sulfuric acid and the sulfuric acid overflowing from the inner tank is allowed to flow into an outer tank Then, a hydrogen peroxide solution is supplied Into the inner tank and the hydrogen peroxide solution is allowed to flow into the outer tank whereby the two kinds of liquids of the hydrogen peroxide solution and the sulfuric acid are stored in the outer tank Simultaneously when the hydrogen peroxide solution flows into the outer tank a return pump is activated. 13-. (canceled)4. A chemical-liquid mixing apparatus for mixing a sulfuric acid and a hydrogen peroxide solution , the apparatus comprising:an inner tank;an outer tank disposed around the inner tank, into which outer tank a liquid overflowing from the inner tank flows;a return pipe configured to return the liquid in the outer tank to the inner tank; anda return pump provided on the return pipe for sending the liquid in the outer tank to the inner tank;a heater provided on the return pipe;a sulfuric-acid supply unit configured to supply a sulfuric acid into the inner tank;a hydrogen-peroxide-solution supply unit configured to supply a hydrogen peroxide solution to the inner tank or the outer tank; anda hydrogen-peroxide-solution replenishing pipe for replenishing a hydrogen peroxide solution that extends through the outer tank to reach an inside of the return pipe such that a hydrogen peroxide solution can be directly fed into the return pipe, with an outlet of the replenishing pipe downstream in the return pipe from an inlet of the return pipe.5. The chemical-liquid mixing apparatus according to claim 4 , further comprisinga controller configured to control the ...

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Номер записи: 70
20-08-2015 дата публикации

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Номер: US20150232395A1
Автор: Black Richard, Cizeron Joel, Czerpak Peter, Faz Carlos, Freer Erik, Harraz Hatem, HONG Jin Ki, Madgavkar Ajay, McCormick Jarod, Michalak William, Nyce Greg, Patel Bipinkumar, Radaelli Guido, Rafique Humera A., Rappold Tim A., Runnebaum Ron, Schammel Wayne, Scher Erik C., Taheri Hassan, Zhang Aihua
Принадлежит:

Integrated systems are provided for the production of higher hydrocarbon compositions, for example liquid hydrocarbon compositions, from methane using an oxidative coupling of methane system to convert methane to ethylene, followed by conversion of ethylene to selectable higher hydrocarbon products. Integrated systems and processes are provided that process methane through to these higher hydrocarbon products. 1. An oxidative coupling of methane (OCM) system , comprising:{'sub': 4', '2+', '2+, '(a) an OCM subsystem that (i) takes as input a feed stream comprising methane (CH) and a feed stream comprising an oxidizing agent, and (ii) generates from said methane and said oxidizing agent a product stream comprising C compounds and non-C impurities;'}{'sub': '2+', '(b) at least one separations subsystem downstream of, and fluidically coupled to, said OCM subsystem, wherein said separations subsystem comprises a first heat exchanger, a de-methanizer unit downstream of said first heat exchanger, and a second heat exchanger downstream of said de-methanizer unit, wherein (i) said first heat exchanger cools said product stream, (ii) said de-methanizer unit accepts said product stream from said first heat exchanger and generates an overhead stream comprising at least a portion of said non-C impurities, and (iii) at least a portion of said overhead stream is cooled in said second heat exchanger and is subsequently directed to said first heat exchanger to cool said product stream; and'}{'sub': '2+', '(c) an olefin to liquids subsystem downstream of said OCM subsystem, wherein said olefin to liquids subsystem is configured to generate higher hydrocarbon(s) from one or more olefins included in said C compounds.'}24.-. (canceled)5. The system of claim 1 , wherein said OCM subsystem comprises at least one OCM reactor claim 1 , and wherein said OCM subsystem comprises at least one post-bed cracking unit downstream of said at least one OCM reactor claim 1 , which post-bed cracking ...

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Номер записи: 71
20-08-2015 дата публикации

METHOD FOR PRODUCING DIMETHYL ETHER AND DEVICE SUITABLE THEREFOR

Номер: US20150232402A1
Автор: Bauer Melanie, Kömpel Harald, Schulz Alexander
Принадлежит: THYSSENKRUPP INDUSTRIAL SOLUTIONS AG

The present disclosure relates to a method and apparatus for producing dimethyl ether by catalytic dehydration of methanol and by distillation of the dehydration product. The method is characterized in that the catalytic dehydration takes place in at least two reaction stages which are connected in series and of which at least the first reaction stage is operated adiabatically, wherein a cooling of the reaction products takes place at least between the first and the second reaction stages. 110.-. (canceled)1121-. (canceled)22. A method for preparing dimethyl ether , comprising: operating the first reaction stage adiabatically, and', 'cooling a reaction product from the first reaction stage before it is further reacted downstream in the second reaction stage; and, 'performing catalytic dehydration of methanol in at least a first reaction stage and a second reaction stage that are connected in series, so as to produce a dehydration product, said performing catalytic dehydration step including,'}distilling the dehydration product.23. The method of claim 22 , wherein said first and second reaction stages are both operated adiabatically.24. The method of claim 22 , wherein said second reaction stage is downstream of said first reaction stage and operated nonadiabatically.25. The method of claim 22 , wherein the second reaction stage is operated adiabatically claim 22 , and wherein a reaction temperature in the first and second reaction stages is between 200 to 400° C.26. The method of claim 22 , wherein during said cooling step between the first and second reaction stages claim 22 , a temperature of the reaction mixture is decreased to a temperature of between 200° C. and 300° C.27. The method of claim 22 , wherein the reaction stages of said performing catalytic dehydration step are carried out in at least two adiabatically operated reactors connected in series claim 22 , and wherein said cooling of the reaction product is performed between the at least two ...

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Номер записи: 72
11-08-2016 дата публикации

Highly efficient neopentyl glycol preparation method and device therefor

Номер: US20160229772A1
Автор: Da Won Jung, Dong Hyun Ko, Mi Young Kim, Min Ji CHOI, Sung Shik Eom, Taeyun Kim
Принадлежит: LG Chem Ltd

Disclosed are a highly efficient neopentyl glycol preparation method and a device therefor. More particularly, disclosed are a method of preparing neopentyl glycol, wherein the method includes adding a hydroxypivaldehyde solution and hydrogen to a hydrogenation reactor that including a hydrogenation catalyst, wherein the hydroxypivaldehyde solution includes 6 to 30% by weight of hydroxypivaldehyde, to 70% by weight of neopentyl glycol, 10 to 30% by weight of alcohol, and 10 to 30% by weight of water, and a device therefor. According to the present disclosure, a neopentyl glycol preparation method wherein separate heating is not required in a section of a feed vessel to an inlet of a hydrogenation reactor unlike conventional technologies to save energy, and, at the same time, by-products with a high boiling point are not generated in the section to prevent poisoning of a hydrogenation catalyst in a reactor due to the by-products with a high boiling point and increase a hydrogenation yield, and a device therefor can be provided.

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Номер записи: 73
11-08-2016 дата публикации

Heat recovery device

Номер: US20160231062A1
Автор: Joon Ho Shin, Sung Kyu Lee, Tae Woo Kim
Принадлежит: LG Chem Ltd

Disclosed are a heat recovery device and a heat recovery method. According to the heat recovery device, it is possible to recovery heat which is discontinuously generated in a batch reactor. In addition, a heat-exchanged heat exchange medium is supplied to a heat storage facility so that various kinds and a great quantity of steams can be produced, if necessary, thereby utilizing these produced steams in various industrial fields.

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Номер записи: 74
10-08-2017 дата публикации

Synthesis of ordered microporous activated carbons by chemical vapor deposition

Номер: US20170225146A1
Автор: Cemal Ercan, Minkee Choi, Rashid M. Othman, Seokin Choi, Yuguo Wang
Принадлежит: Korea Advanced Institute of Science and Technology KAIST, Saudi Arabian Oil Co

Embodiments provide a methane microporous carbon adsorbent including a thermally-treated CVD carbon having a shape in the form of a negative replica of a crystalline zeolite has a BET specific surface area, a micropore volume, a micropore to mesopore volume ratio, a stored methane value and a methane delivered value and a sequential carbon synthesis method for forming the methane microporous carbon adsorbent. Introducing an organic precursor gas for a chemical vapor deposition (CVD) period to a crystalline zeolite that is maintained at a CVD temperature forms the carbon-zeolite composite. Introducing a non-reactive gas for a thermal treatment period to the carbon-zeolite composite maintained at a thermal treatment temperature forms the thermally-treated carbon-zeolite composite. Introducing an aqueous strong mineral acid mixture to the thermally-treated carbon-zeolite composite forms the methane microporous carbon adsorbent.

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Номер записи: 75
10-08-2017 дата публикации

TRANSPORTABLE LIQUID PRODUCED FROM NATURAL GAS

Номер: US20170226431A1
Автор: SCHECHNER PINCHAS
Принадлежит:

A system and a method for converting Natural Gas (NG) to high energy transportable liquid (such as gasoline) are disclosed. A semiconductor UV-source is used for initiate a photo lytic reaction between methane molecules and photons having energy equal or bigger than the energy of dissociation of the C—H bond in methane. The formed radicles are further react to produce higher molecular weight hydrocarbons, while hydrogen gas is separates from the reaction mixture in order to avoid reverse reactions. 118-. (canceled)19. A method for the conversion of methane into high-energy room temperature liquids , comprising the steps of:introducing methane into a closed volume;irradiating said methane with at least one semiconductor UV radiation source, selected from the group comprising an LED and a LASER, in order to produce photochemical, radical and molecular collision chemical reactions, so as to obtain mixtures of chemical liquid products and chemical gaseous products that include hydrogen, ethane, propane, butane isomers, pentane isomers, hexane isomers, heptane isomers, octane isomers, nonane isomers, and decane isomers;collecting said hydrogen, that is separated from said mixture by one selected from a group comprising buoyancy, a hydrogen selective membrane, and a centrifugal gas separator, within an upper portion of said closed volume and extracting said collected hydrogen from said closed volume through an outlet dedicated to the extraction of hydrogen;using said separated hydrogen to produce electricity that activates at least one electricity consuming load that is to be used by the method's procedure;collecting said liquid products, that condense at room temperature, at the bottom of said closed volume;extracting said collected liquids from said closed volume through an outlet dedicated to the extraction of liquid products;repeating said previous steps upon the remaining gaseous mixture in said closed volume; andadding methane so as to maintain constant pressure ...

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Номер записи: 76
19-08-2021 дата публикации

HYDROGEN REFORMING SYSTEM

Номер: US20210252471A1
Автор: Park Jung Joo
Принадлежит:

A hydrogen reforming system includes: a steam reforming system (i) receiving a raw material gas and reacting the raw material gas with water to generate a first mixed gas containing hydrogen, (ii) reacting the first mixed gas with the water to separate the first mixed gas into hydrogen and carbon dioxide, and (iii) discharging hydrogen and carbon dioxide; a dry reforming system (i) receiving and reacting the raw material gas and the carbon dioxide discharged from the steam reforming system to generate a second mixed gas containing hydrogen, (ii) reacting the second mixed gas with the water to separate the second mixed gas into hydrogen and carbon dioxide, and (iii) discharge hydrogen and carbon dioxide; and a water supply device supplying the water to the steam reforming system and the dry reforming system. 1. A hydrogen reforming system comprising:a steam reforming system configured to (i) receive a raw material gas and react the raw material gas with water to generate a first mixed gas containing hydrogen, (ii) react the first mixed gas with the water to separate the first mixed gas into hydrogen and carbon dioxide, and (iii) discharge hydrogen and carbon dioxide;a dry reforming system configured to (i) receive and react the raw material gas and the carbon dioxide discharged from the steam reforming system to generate a second mixed gas containing hydrogen, (ii) react the second mixed gas with the water to separate the second mixed gas into hydrogen and carbon dioxide, and (iii) discharge hydrogen and carbon dioxide; anda water supply device configured to supply the water to the steam reforming system and the dry reforming system.2. The hydrogen reforming system of claim 1 , wherein the water supply device is connected to be heat-exchangeable with the steam reforming system and the dry reforming system claim 1 , andthe water is heated by heat exchange while flowing through the water supplying device to supply thermal energy to the steam reforming system and the ...

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Номер записи: 77
25-07-2019 дата публикации

METHOD AND SYSTEM FOR POLYMERIZING ACRYLATES

Номер: US20190225713A1
Автор: Fischer Wolfgang, Ittemann Peter, PATCAS Florian, RUF Michael
Принадлежит:

The invention relates to a method for polymerizing acrylates using a reactor (). Reaction heat produced in the reactor () is discharged via a boiling cooler () in that gaseous vapors produced in the reactor () are supplied to the boiling cooler (), and condensed vapors are returned to the reactor () from the boiling cooler (). At least one component containing acrylate is at least partly added via the boiling cooler () and reaches the reactor () via the boiling cooler (). The invention additionally relates to a system for polymerizing an acrylate, comprising a reactor () and a boiling cooler () for discharging reaction heat produced in the reactor (). The boiling cooler () has at least one filling opening () for supplying at least one component containing acrylate. 117-. (canceled)18. A process for polymerizing acrylates by a reactor , whereheat of reaction arising in the reactor is removed by an evaporative cooler by feeding gaseous vapor formed in the reactor to the evaporative cooler and recirculating condensed vapor from the evaporative cooler to the reactor,wherein at least one component containing acrylate is introduced at least partly via the evaporative cooler and goes via the evaporative cooler into the reactor,wherein a reduced pressure, in particular in the range from 150 mbar to 350 mbar, is generated in the reactor,wherein a reduced pressure compared to atmospheric pressure prevails in the reactor during the polymerization of the acrylate.19. The process of claim 18 , wherein the at least one component contains butyl acrylate.20. The process of claim 18 , wherein a further component containing a monomer having two double bonds is at least partly introduced into the evaporative cooler.21. The process of claim 18 , wherein the at least one component is at least partly introduced from above through a cap of the evaporative cooler.22. The process of claim 18 , wherein the at least one component is at least partly introduced from above into a plurality of ...

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Номер записи: 78
03-09-2015 дата публикации

REFORMATE HYDROTREATMENT METHOD

Номер: US20150247098A1
Автор: Chen Qingling, HE Xiaojun, JIANG Lei, Li Hua, Li Qinghua, LIU Chengli, Liu Jianping, She Xichun, Yang Qingpin, Zeng Zhiyu
Принадлежит: CHINA PETROLEUM & CHEMICAL CORPORATION

Provided is a reformate hydrotreatment method, the method comprising: under liquid phase hydrotreatment conditions, bringing the reformate and a catalyst having a catalytic hydrogenation effect into contact in a hydrogenation reactor, the hydrogen used in the hydrotreating process at least partially coming from the hydrogen dissolved in the reformate. According to the method of the present invention, the reformate separated from a reformate products separating tank can directly undergo liquid phase hydrotreatment; therefore not only can the hydrogen dissolved in the reformate be fully utilized, but the olefins in the reformate can also be removed, while eliminate the requirements for recycle hydrogen and a recycle device thereof. The reformate obtained by the method of the present invention reduces the bromine index to below 50 mgBr/100 g, and has an arene loss of less than 0.5 wt %. 1. A method for hydroprocessing reformate , comprising contacting reformate with a catalyst having a catalytic hydrogenation action under a liquid-phase hydroprocessing condition in a hydrogenation reactor , at least part of hydrogen gas for hydroprocessing is from dissolved hydrogen contained in the reformate.2. The method according to claim 1 , wherein the hydroprocessing is carried out in presence of supplemental hydrogen gas claim 1 , the supplemental hydrogen gas is hydrogen gas injected into the reformate in one time or in several times before contacting and/or during contacting.3. The method according to claim 2 , wherein the supplemental hydrogen gas is injected into the reformate through pores with an average pore diameter in nanometer size.4. The method according to claim 3 , wherein the supplemental hydrogen gas is injected into the reformate through pores with an average pore diameter in nanometer size by means of a mixing device claim 3 , the mixing device comprises at least one liquid passage for accommodating the reformate and at least one gas passage for accommodating ...

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Номер записи: 79
25-08-2016 дата публикации

JET LOOP REACTOR WITH NANOFILTRATION AND GAS SEPARATOR

Номер: US20160243519A1
Автор: Franke Robert, Hamers Bart
Принадлежит:

The invention relates to a device for the continuous homogeneous catalytic reaction of a liquid with a gas and optionally a further fluid, wherein the device comprises at least one jet loop reactor having an external liquid circuit driven by at least one pump, and wherein the device has at least one membrane separation unit, preferably retaining the homogeneous catalyst, which membrane separation unit is arranged in the external liquid circuit of the jet loop reactor. The object thereof is to reduce the costs of the device. This is achieved by providing an additional apparatus, namely a gas separator, which is arranged in the external liquid circuit of the jet loop reactor and is installed for separating off gas from the external liquid circuit and feeding it back into the jet loop reactor. 1. A device for the continuous homogeneous catalytic reaction of a liquid with a gas and optionally a further fluid , wherein the device comprises at least one jet loop reactor having an external liquid circuit driven by at least one pump , and wherein the device has at least one membrane separation unit , preferably retaining the homogeneous catalyst , which membrane separation unit is arranged in the external liquid circuit of the jet loop reactor , wherein a gas separator is arranged in the external liquid circuit of the jet loop reactor , which gas separator is installed for separating off gas from the external liquid circuit and feeding it back into the jet loop reactor.2. The device according to claim 1 , wherein in the external liquid circuit claim 1 , upstream of the membrane separation unit claim 1 , a heat exchanger is arranged for cooling the feed of the membrane separation unit claim 1 , and in that the gas separator is arranged downstream of the heat exchanger upstream of the membrane separation unit.3. The device according to claim 1 , wherein the pump is arranged upstream of the membrane separation unit claim 1 , in particular in that it is arranged upstream of the ...

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Номер записи: 80
23-08-2018 дата публикации

NOVEL PROCESS FOR METHANOL PRODUCTION FROM LOW QUALITY SYNTHESIS GAS

Номер: US20180237366A1
Автор: Modarresi Hassan
Принадлежит: Haldor Topsoe A/S

In a novel process for methanol production from low quality synthesis gas, in which relatively smaller adiabatic reactors can be operated more efficiently, some of the inherent disadvantages of adiabatic reactors for methanol production are avoided. This is done by controlling the outlet temperature in the pre-converter by rapid adjustment of the recycle gas, i.e. by manipulating the gas hourly space velocity in the pre-converter. 1. A process for methanol production from synthesis gas comprising the following steps:providing a fresh, pressurized methanol synthesis gas containing hydrogen, carbon monoxide and carbon dioxide, which is pre-heated and passed through a methanol pre-converter/guard reactor, in which the synthesis gas is partially converted to methanol over a heterogeneous methanol catalyst and poisonous impurities are removed from the feed gas,providing a recycle gas stream containing partly converted methanol synthesis gas and mixing a part of the recycle stream with the fresh synthesis gas if necessary, such as in case of part load, to a process gas stream,cooling the process gas stream from the pre-converter/guard reactor to a temperature, which is suitable for the main converter, and passing the cooled process gas stream to a conventional methanol synthesis loop, andseparating raw methanol from the synthesis loop,wherein the outlet adiabatic temperature in the pre-converter/guard reactor is controlled by rapid adjustment of the recycle gas, i.e. by manipulation of the GHSV (gas hourly space velocity) in the pre-converter.2. Process according to claim 1 , wherein the pre-converter/guard reactor(s) is/are sized and designed for the plant full load condition claim 1 , treating and converting the inlet feed gas (make-up gas) without risk of catalyst overheating.3. Process according to claim 2 , wherein a safe gas space velocity is established across the reactor in the methanol synthesis loop to avoid overheating of the catalyst.4. Process according to ...

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Номер записи: 81
13-11-2014 дата публикации

PROCESS AND APPARATUS FOR HEAT RECOVERY IN VINYL CHLORIDE MONOMER PLANTS OR IN INTEGRATED VINYL CHLORIDE MONOMER OR POLYVINYL CHLORIDE PLANTS

Номер: US20140336426A1
Автор: Benje Michael, Kammerhofer Peter
Принадлежит:

Disclosed is a process and apparatus for heat recovery in vinyl chloride monomer manufacturing plants or in integrated vinyl chloride monomer/polyvinyl chloride manufacturing plants. A process for capture and use of excess heat recovered in the production of vinyl chloride includes distillatively purifying DCE in a high-boilers column, using a heat exchanger to capture thermal energy from a purified DCE vapor stream from the high-boilers column, generating low pressure steam from the captured thermal energy, returning condensed DCE vapors to the high-boilers column, and heating parts of the plant with the generated low pressure steam. 112.-. (canceled)13. A process for the capture and use of excess heat recovered during the production of vinyl chloride by the thermal cleavage of 1 ,2-dichloroethane in a vinyl chloride manufacturing complex that incorporates distillative purification of 1 ,2-dichloroethane using at least one high-boilers column in which substances boiling at temperatures higher than the boiling point of 1 ,2-dichloroethane are removed , the process comprising:distillatively purifying 1,2-dichloroethane by boiling 1,2-dichloroethane at temperatures between 120-150° C. in a high-boilers column of the vinyl chloride manufacturing complex to create a 1,2-dichloroethane vapor stream;capturing thermal energy from at least a portion of a distillatively purified 1,2-dichloroethane vapor stream, by at least one heat exchanger associated with at least one of a plant component dedicated to producing 1,2-dichloroethane, a downstream plant component dedicated to producing vinyl chloride, or a downstream plant component dedicated to producing polyvinyl chloride;generating low-pressure steam from the thermal energy captured by the heat exchanger;returning the 1,2-dichloroethane vapor into the high-boilers column following a condensation thereof; andheating selected parts of the plant with the generated low pressure steam.14. The process of claim 13 , wherein the at ...

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Номер записи: 82
30-08-2018 дата публикации

METHOD AND DEVICE FOR PRODUCING SULFURIC ACID

Номер: US20180244522A1
Автор: GUETTA Zion, Thielert Holger
Принадлежит:

In a production mode a process for preparing sulfuric acid may involve oxidizing sulfur to sulfur dioxide in a first oxidation stage, and catalytically oxidizing the sulfur dioxide to sulfur trioxide in a second oxidation stage. The sulfur trioxide may be absorbed in at least one absorption stage. In the production mode, process gases from a last of the at least one absorption stage with respect to a flow direction are discharged. In a standby mode of the process, at least one heating stage for heating the process gases is connected. The process gases exiting from the at least one absorption stage are conveyed to the heating stage, and the process gases are circulated via the heating stage, the second oxidation stage, and the absorption stage. 110.-. (canceled)12. The process of wherein in the production mode the process comprises feeding sulfur and air for the oxidation to the first oxidation stage claim 11 , wherein in the standby mode the process comprises stopping the feeding of sulfur and at least throttling back on the feeding of air.13. The process of wherein in the standby mode the process comprises conveying the process gases from the at least one absorption stage claim 11 , bypassing the first oxidation stage claim 11 , to the heating stage and from the heating stage to the second oxidation stage.14. The process of wherein the process gases are claim 11 , after passing through a first part of the second oxidation stage claim 11 , discharged from the second oxidation stage andin the production mode of the process, conveyed through an intermediate absorption stage of the at least one absorption stage and subsequently recirculated to the second oxidation stage where the process gases pass through a second part of the second oxidation stage, andin the standby mode of the process, recirculated via a closeable bypass conduit to the second oxidation stage, bypassing the intermediate absorption stage.15. The process of wherein after the process gases pass through ...

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Номер записи: 83
08-08-2019 дата публикации

Apparatus and Process for the Hydroconversion of Heavy Oil Products

Номер: US20190241820A1
Автор: Bonomi Susi, Molinari Mario
Принадлежит:

The present invention relates to an apparatus for the hydroconversion of heavy oil products (the fresh load). Said apparatus comprises: a slurry bubble column hydroconversion reactor, which comprises a feed line in which the fresh load and the recirculated slurry phase are conveyed, an inlet line for a hydrogenating stream and an outlet for a reaction effluent through an outlet nozzle; a stripping column at high pressure and high temperature placed downstream of the reactor and directly connected to the reactor head through a pipeline in which the reaction effluent flows; said column having an inlet line for a stripping gas, an inlet for the reactor effluent, a head outlet for steam and an outlet for the slurry phase; lines and means for recirculating the slurry leaving the stripping column; lines and means for taking a drain stream, which has the function of preventing the accumulation of solids in the reactor. The stripping column is characterized in that it contains one or more contact devices that allow physical contact to be created between different phases. 1. Apparatus for the hydroconversion of heavy oil products which constitute the fresh load , said apparatus comprising:a slurry bubble column hydroconversion reactor, which comprises a feed line in which the fresh load and the recirculated slurry phase are conveyed, an inlet line for a hydrogenating stream and an outlet for a reaction effluent through an outlet nozzle;a high pressure and high temperature stripping column placed downstream of the reactor and directly connected to the reactor head through a pipeline in which the reaction effluent flows; said column having an inlet line for a stripping gas, an inlet for the reactor effluent, a head outlet for steam and an outlet for the slurry phase;lines and means for recirculating the slurry leaving the stripping column;lines and means for taking a drain stream, which has the function of preventing the accumulation of solids in the reactor;said stripping ...

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Номер записи: 84
30-07-2020 дата публикации

Ways to Prevent Pump-Around Heat Exchanger Fouling and Extend Run Lengths on a Benzene Hydrogenation Unit

Номер: US20200239385A1
Автор: Garcia Israel, Snell Ryan W.
Принадлежит:

A process for hydrogenation of an aromatic hydrocarbon including introducing a hydrocarbon feed comprising the aromatic hydrocarbon, a hydrogen feed comprising hydrogen, and a hydrogenation catalyst into a hydrogenation reactor operable with a liquid phase and a gas phase to produce a hydrogenation product; removing a gas phase product stream comprising the hydrogenation product; withdrawing a portion of the liquid phase; subjecting the withdrawn portion to heat exchange to provide a reduced-temperature withdrawn portion; introducing the reduced-temperature withdrawn portion back into the hydrogenation reactor; and at least one of: (a) providing at least two heat exchangers to effect the subjecting of the withdrawn portion of the liquid phase to heat exchange; (b) separating a decomposition product of the hydrogenation catalyst, the hydrogenation catalyst, or both, from the withdrawn portion of the liquid phase prior to the heat exchange; and (c) reducing exposure of the hydrogenation catalyst to an oxygen-containing species. 120-. (canceled)21. A system for liquid phase hydrogenation , the system comprising:a hydrogenation reactor operable with a liquid phase and a gas phase to convert an aromatic hydrocarbon in a hydrocarbon feed to a hydrogenation product by contacting the aromatic hydrocarbon with hydrogen in a hydrogen feed in the presence of a hydrogenation catalyst;a pump-around loop comprising a pump configured to move a withdrawn portion of the liquid phase from the hydrogenation reactor through the pump-around loop and back to the hydrogenation reactor;at least one primary heat exchanger after the pump in the pump-around loop wherein the primary heat exchanger is configured to reduce the temperature of at least a portion of the liquid phase withdrawn from the hydrogenation reactor, thus providing a reduced-temperature withdrawn portion, prior to introduction of the reduced-temperature withdrawn portion into the hydrogenation reactor; and(a) at least one ...

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Номер записи: 85
15-09-2016 дата публикации

PNEUMATICALLY AGITATED IONIC LIQUID ALKYLATION USING VAPORIZATION TO REMOVE REACTION HEAT

Номер: US20160263547A1
Автор: Chang Bong-Kyu, Girgis Michael John, Lowe Clifford Michael, Luo Huping, Mohr Donald Henry, Parimi Krishniah, Timken Hye Kyung Cho
Принадлежит:

Systems and apparatus for ionic liquid catalyzed hydrocarbon conversion, such as alkylation, using vaporization to remove reaction heat from an ionic liquid reactor and to provide mixing therein, wherein hydrocarbon vapors are withdrawn from the ionic liquid reactor and the withdrawn hydrocarbon vapor is recovered by a hydrocarbon vapor recovery unit in fluid communication with the ionic liquid reactor for recycling condensed hydrocarbons to the ionic liquid reactor. Processes for ionic liquid catalyzed alkylation are also disclosed. 1. A system , comprising:an ionic liquid reactor configured for performing an ionic liquid catalyzed exothermic hydrocarbon conversion reaction, wherein the ionic liquid reactor comprises a hydrocarbon vapor outlet configured for withdrawing hydrocarbon vapor from the ionic liquid reactor;at least one ionic liquid injection nozzle disposed within the ionic liquid reactor, each said ionic liquid injection nozzle configured for injecting ionic liquid catalyst into the ionic liquid reactor;at least one hydrocarbon feed injection unit disposed within the ionic liquid reactor, each said hydrocarbon feed injection unit configured for injecting a hydrocarbon feed stream into the ionic liquid reactor;a hydrocarbon vapor recovery unit in fluid communication with the hydrocarbon vapor outlet, wherein the hydrocarbon vapor recovery unit is configured for receiving hydrocarbon vapor withdrawn from the ionic liquid reactor and for condensing the withdrawn hydrocarbon vapor to provide a condensed hydrocarbon liquid stream; anda condensed hydrocarbon liquid conduit, in fluid communication with the hydrocarbon vapor recovery unit, configured for recycling the condensed hydrocarbon liquid stream to the ionic liquid reactor.2. The system according to claim 1 , wherein:the ionic liquid reactor is substantially cylindrical,the ionic liquid reactor is oriented in an orientation selected from the group consisting of vertically oriented and horizontally ...

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Номер записи: 86
15-08-2019 дата публикации

Metallocene Catalyst Feed System for Solution Polymerization Process

Номер: US20190247821A1
Автор: Jay L. Reimers, Keith C. Gallow, Vetkav R. Eswaran
Принадлежит: ExxonMobil Chemical Patents Inc

Methods and systems for solution polymerization. The method can include forming a first mixture stream consisting essentially of at least one catalyst and a process solvent, and forming a second mixture stream consisting essentially of at least one activator and the process solvent. The first mixture stream and the second mixture stream can be fed separately to at least one reaction zone comprising one or more monomers dissolved in the process solvent where the at least one monomers can be polymerized within the at least one reaction zone in the presence of the catalyst, activator and process solvent to produce a polymer product.

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Номер записи: 87
15-09-2016 дата публикации

LIQUID FUEL REFORMER INCLUDING A VAPORIZER AND METHOD OF REFORMING LIQUID REFORMABLE FUEL

Номер: US20160264414A1
Автор: Dewald Paul, Finnerty Caine M.
Принадлежит:

A liquid fuel reformer () includes a fuel vaporizer () which utilizes heat from an upstream source of heat, specifically, an electric heater (), operable in the start-up mode of the reformer (), and therefore independent of the reforming reaction zone of the reformer, to vaporize fuel in a downstream vaporization zone. 1. A liquid fuel reformer system for the production of hydrogen-rich reformate , the liquid fuel reformer system comprising:a liquid fuel reformer comprising a reformer inlet;a conduit comprising an oxygen-containing gas inlet, a liquid reformable fuel inlet located downstream from the oxygen-containing gas inlet, and a gaseous reaction mixture outlet located downstream from the liquid reformable fuel inlet, wherein the conduit provides fluid communication among the oxygen-containing gas inlet, the liquid reformable fuel inlet and the gaseous reaction mixture outlet, and the gaseous reaction mixture outlet is in fluid communication with the reformer inlet;a first source of heat comprising an electric heater, the first source of heat being disposed in the conduit at a location downstream from the oxygen-containing gas inlet and upstream from the liquid reformable fuel inlet;a second source of heat comprising heat of exotherm from the liquid fuel reformer and/or a hydrogen reformate-consuming device external to the liquid fuel reformer, the second source of heat in thermal communication with the conduit and at a location downstream from the first source of heat upstream from the liquid reformable fuel inlet; anda vaporizer, the vaporizer being disposed in the conduit at a location downstream from the liquid reformable fuel inlet, or defining the liquid reformable fuel inlet.2. The liquid fuel reformer system of comprising:a third source of heat comprising an electric heater, the third source of heat being disposed in the conduit at a location downstream from the first and second sources of heat and upstream from the liquid reformable fuel inlet;3. The ...

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Номер записи: 88
15-09-2016 дата публикации

ETHYLBENZENE DEHYDROGENATION PLANT FOR PRODUCING STYRENE AND RELATIVE PROCESS

Номер: US20160264496A1
Автор: GALEOTTI Armando, OLIOSI Mirko
Принадлежит: Versalis S.p.A.

An ethylbenzene dehydrogenation plant for producing styrene which comprises a reaction section in which one or more adiabatic reaction apparatuses are positioned in series, and a steam circuit in which there is at least one first steam heat exchange apparatus; said plant being characterized in that it comprises heating equipment in which there is a heating circuit by means of recirculation of the fumes formed during dehydrogenation processes of ethylbenzene to give styrene, wherein said heating equipment comprises the following apparatuses in fluid communication with each other by means of said heating circuit: one or more ultra-heating apparatuses, one or more combustion devices in which at least one steam diffuser, one burner and at least one mixing apparatus are inserted, one or more ventilation device(s). 1. An ethylbenzene dehydrogenation plant for producing styrene which comprises a reaction section in which one or more adiabatic reaction devices are positioned in series , and a steam circuit in which there is at least one first steam heat exchange apparatus; said plant being characterized in that it comprises heating equipment in which there is a heating circuit by means of recirculation of the fumes formed during dehydrogenation processes of ethylbenzene to give styrene , wherein said heating equipment comprises the following apparatuses in fluid communication with each other by means of said heating circuit:one or more ultra-heating apparatuses,one or more combustion devices in which at least one steam diffuser, one burner and at least one mixing apparatus are inserted,one or more ventilation devices.2. The dehydrogenation plant according to claim 1 , wherein the heating equipment in which there is a heating circuit by means of recirculation of the fumes claim 1 , is positioned between one adiabatic reactor and a subsequent adiabatic reactor claim 1 , said reactors being in series.3. The dehydrogenation plant according to claim 1 , wherein the heating ...

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Номер записи: 89
15-09-2016 дата публикации

Installation and method for producing fatty acid esters usable as fuel

Номер: US20160264911A1
Автор: Maria Úrsula CHORNET SERRANO, Pau AZKARATE CAPELL
Принадлежит: Supercritical Ideas Sl

Installation and method for producing fatty acid esters usable as fuel for which the installation includes a tank ( 10 ) containing oils and/or fats to be treated, a tank ( 11 ) containing light alcohol, pumps ( 3 ) and ( 4 ) feeding the materials to a tubular reaction vessel ( 30 ) having a winding configuration provided with a heater for internally maintaining a supercritical temperature with respect to the alcohol used and a pressure provided by the pumps, suitable for producing esterification and transesterification reactions, without the presence of catalysts of the oils and/or fats and alcohol, a heat exchanger ( 8 ) for heating the affluents and cooling the reaction effluents and a reaction effluent depressurization tank ( 21 ). The installation further has a stirrer ( 22, 23, 28 ) for stirring the reaction product at the reaction temperature and pressure in one or more segments of the tubular vessel ( 30 ) covering a sector of the reactor before its end area for exit towards the depressurization tank ( 21 ).

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Номер записи: 90
27-11-2014 дата публикации

Hydroformylation process

Номер: US20140350305A1
Автор: Glenn A. Miller, James D. DUSTON, Michael C. Becker, Steven H. FISHER, Victoria L. BIEDENSTEIN
Принадлежит: DOW TECHNOLOGY INVESTMENTS LLC

Disclosed is an improved exothermic hydroformylation process having at least two reaction stages. Cooling is provided by externally cooling a stream of reaction mixture from one of the stages, dividing the cooled stream into at least two cooled reaction mixture streams; transferring one cooled reaction mixture stream back into the same reaction stage from which it was removed to cool the reaction mixture in that reaction stage; and transferring at least one cooled reaction mixture stream(s) into and through heat exchange means that cool a different reaction stage, and returning it to the same reaction stage from which it was removed.

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Номер записи: 91
01-10-2015 дата публикации

METHOD FOR THE PRODUCTION OF ALKENYL HALOSILANES, AND REACTOR SUITED THEREFOR

Номер: US20150274758A1
Автор: Bade Stefan, Schladerbeck Norbert
Принадлежит: Evonik Industries AG

Described is a method for producing alkenyl halosilanes by reacting alkenyl halide selected from the group comprising vinyl halide, vinylidene halide, and allyl halide with halosilane selected from the group comprising monohalosilane, dihalosilane, and trihalosilane in the gas phase in a reactor comprising a reaction tube () that has an inlet () at one end and an outlet () at the other end, said reactor further comprising an annular-gap nozzle () that is mounted on the inlet (), extends into the reaction tube (), and has a central supply duct () for one reactant () and a supply duct (), which surrounds the central supply duct (), for the other reactant (). In order to carry out said method, alkenyl halide is injected into the reaction tube () through the central supply duct (), halosilane is injected thereinto through the surrounding supply duct (), and both substances flow through the reaction tube () in the direction of the outlet (). The described method allows alkenyl halosilanes to be produced at a high yield and with great selectivity. The amount of soot formed is significantly lower than in conventional reators. The invention also relates to a reactor for carrying out gas-phase reactions, said reactor being characterized by at least the following elements: A) a reaction tube () that has B) an inlet () at one end, C) an outlet () at the other end, and D) an annular-gap nozzle () which includes a central supply duct () for one reactant () and a supply duct (), which surrounds the central supply duct (), for another reactant (), said nozzle being mounted on the inlet () and extending into the reaction tube (). 11234576582115613. Process for preparing alkenylhalosilanes by reacting alkenyl halide selected from the group of vinyl halide , vinylidene halide and allyl halide with halosilane selected from the group of mono- , di- and trihalosilane in the gas phase in a reactor comprising a reaction tube () equipped with an inlet () at one end of the tube and with an ...

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Номер записи: 92
22-08-2019 дата публикации

Ways to Prevent Pump-Around Heat Exchanger Fouling and Extend Run Lengths on a Benzene Hydrogenation Unit

Номер: US20190256443A1
Автор: Garcia Israel, Snell Ryan W.
Принадлежит:

A process for hydrogenation of an aromatic hydrocarbon including introducing a hydrocarbon feed comprising the aromatic hydrocarbon, a hydrogen feed comprising hydrogen, and a hydrogenation catalyst into a hydrogenation reactor operable with a liquid phase and a gas phase to produce a hydrogenation product; removing a gas phase product stream comprising the hydrogenation product; withdrawing a portion of the liquid phase; subjecting the withdrawn portion to heat exchange to provide a reduced-temperature withdrawn portion; introducing the reduced-temperature withdrawn portion back into the hydrogenation reactor; and at least one of: (a) providing at least two heat exchangers to effect the subjecting of the withdrawn portion of the liquid phase to heat exchange; (b) separating a decomposition product of the hydrogenation catalyst, the hydrogenation catalyst, or both, from the withdrawn portion of the liquid phase prior to the heat exchange; and (c) reducing exposure of the hydrogenation catalyst to an oxygen-containing species. 1. A process for liquid phase hydrogenation of an aromatic hydrocarbon , the process comprising:introducing a hydrocarbon feed comprising the aromatic hydrocarbon, a hydrogen feed comprising hydrogen, and a hydrogenation catalyst into a hydrogenation reactor operable with a liquid phase and a gas phase, whereby at least a portion of the aromatic hydrocarbon is hydrogenated to produce a hydrogenation product;removing, from the hydrogenation reactor, a gas phase product stream comprising the hydrogenation product;withdrawing, from the hydrogenation reactor, a portion of the liquid phase;subjecting at least a portion of the withdrawn portion of the liquid phase to heat exchange, thus providing a reduced-temperature withdrawn portion;introducing the reduced-temperature withdrawn portion back into the hydrogenation reactor;providing at least two heat exchangers to effect the subjecting of the withdrawn portion of the liquid phase to heat exchange, ...

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Номер записи: 93
29-09-2016 дата публикации

Reformer with perovskite as structural component thereof

Номер: US20160280541A1
Автор: Caine M. Finnerty, Paul DEWALD
Принадлежит: WATT Fuel Cell Corp

A reformer includes at least one reformer reactor unit ( 300 ) having a space-confining wall with external ( 307 ) and internal surfaces ( 306 ), at least a section of the wall and space confined thereby defining a reforming reaction zone ( 311 ), an inlet end ( 301 ) and associated inlet ( 302 ) for admission of flow of gaseous reforming reactant to the reforming reaction zone ( 311 ), an outlet end ( 303 ) and associated outlet ( 304 ) for outflow of hydrogen-rich reformate produced in the reforming reaction zone ( 311 ), at least that section of the wall ( 305 ) corresponding to the reforming reaction zone comprising perovskite as a structural component thereof such wall section being gas-permeable to allow gaseous reforming reactant to diffuse therein and hydrogen-rich reformate to diffuse therefrom.

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Номер записи: 94
27-09-2018 дата публикации

COOLING BETWEEN MULTIPLE POLYOLEFIN POLYMERIZATION REACTORS

Номер: US20180272309A1
Автор: BENHAM Elizabeth A., Bhandarkar Maruti, Gill Catherine M., GONZALES Rebecca A., Kufeld Scott E., MUTCHLER Joel A., Nguyen Thanh T., Odi Timothy O.
Принадлежит: CHEVRON PHILLIPS CHEMICAL COMPANY LP

A system and method for a first reactor to produce a transfer slurry having a first polyolefin polymerized in the first reactor, a heat-removal zone to remove heat from the transfer slurry, and a second reactor to receive the transfer slurry cooled by the heat-removal zone, the second reactor to produce a product slurry having a product polyolefin which includes the first polyolefin and a second polyolefin polymerized in the second reactor. 114.-. (canceled)15. A method of operating a polyolefin manufacturing system , comprising:producing a first polyolefin in a first polymerization reactor;discharging from the first polymerization reactor a transfer slurry comprising the first polyolefin;cooling the transfer slurry to produce a second reactor transfer feed slurry;introducing the second reactor transfer feed slurry into a second polymerization reactor;producing a second polyolefin in the second polymerization reactor; anddischarging from the second polymerization reactor a second reactor discharge slurry comprising the first polyolefin and the second polyolefin,wherein the transfer slurry and the second reactor transfer feed slurry have a temperature difference of at least 3° F.,wherein the transfer slurry is not recycled into the transfer slurry or the first polymerization reactor, andwherein the second reactor discharge slurry is not recycled into the transfer slurry, the second reactor transfer feed, the first polymerization reactor, or the second polymerization reactor.16. The method of claim 15 , wherein cooling the transfer slurry comprises receiving a cooling medium to cool the transfer slurry.17. The method of claim 15 , comprising receiving a cooling medium at a heat exchanger claim 15 , and wherein cooling the transfer slurry comprises subjecting the transfer slurry to the heat exchanger.18. The method of claim 15 , comprising routing the transfer slurry through a first portion of a transfer line to a heat exchanger claim 15 , and wherein cooling the ...

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Номер записи: 95
27-09-2018 дата публикации

ENERGY SAVING METHOD AND APPARATUS FOR PREPARING STYRENE AND ALPHA-METHYLSTYRENE CONCURRENTLY

Номер: US20180273445A1
Автор: Kim Mi-Kyung, Lee Jae-Ik, LEE Jeong-Seok, Lee Jong-Ku
Принадлежит: LG CHEM, LTD.

The present invention relates to energy saving method and apparatus for preparing styrene and alpha-methylstyrene concurrently, by which economic feasibility may be improved by reusing energy during preparing styrene and alpha-methylstyrene concurrently. 1. A method for preparing styrene and alpha-methylstyrene concurrently , the method comprising:(a) a step of performing dehydrogenation reaction of ethylbenzene and cumene in the presence of a catalyst;(b) a step of recovering heat from a reaction product by the reaction;(c) a step of separating a gas phase from at least a portion of a reaction product undergone step (b) and sending thereof to a compression part, separating condensing water including water from a liquid phase, and recovering a fraction including styrene and alpha-methylstyrene;(d) a step of compressing and cooling at least a portion of a gas phase among reaction products undergone step (c) to separate components having a low boiling point including hydrogen and carbon dioxide as a gas phase, and recycle a liquid phase including styrene, alpha-methylstyrene, ethylbenzene and cumene to step (c);(e) a step of distilling and separating at least a portion of the fraction including styrene and alpha-methylstyrene, which is recover in step (c), into a fraction including styrene and a fraction including unreacted cumene;(f) a step of recovering styrene from at least a portion of the fraction including styrene of step (e) and distilling and separating the fraction including unreacted ethylbenzene;(g) a step of recovering ethylbenzene from at least a portion of the fraction including unreacted ethylbenzene of step (f) and recycling to a reaction part, and distilling and separating the fraction including benzene and toluene;(h) a step of recovering cumene from at least a portion of the fraction including unreacted cumene of step (e) and recycling the recovered cumene to a reaction part, and distilling and separating a fraction including alpha-methylstyrene; ...

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Номер записи: 96
15-10-2015 дата публикации

Process and Apparatus for Continuous Solution Polymerization

Номер: US20150290616A1
Автор: Periagaram S. Ravishankar, Quintin P. COSTIN
Принадлежит: ExxonMobil Chemical Patents Inc

Provided are processes and apparatuses for continuous solution polymerization which can mitigate fouling during the production of propylene-based polymers.

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Номер записи: 97
15-10-2015 дата публикации

REACTORS AND METHODS FOR PRODUCING SOLID CARBON MATERIALS

Номер: US20150291424A1
Автор: Noyes Dallas B.
Принадлежит:

A reactor for producing a solid carbon material comprising at least one reaction chamber configured to produce a solid carbon material and water vapor through a reduction reaction between at least one carbon oxide and at least one gaseous reducing material in the presence of at least one catalyst material. Additional reactors, and related methods of producing a solid carbon material, and of forming a reactor for producing a solid carbon material are also described. 1. A reactor for producing a solid carbon material , comprising:at least one reaction chamber configured to produce a solid carbon material and water vapor through a reduction reaction between at least one carbon oxide and at least one gaseous reducing material in the presence of at least one catalyst material; andat least one cooling chamber operatively communicating with the at least one reaction chamber and configured to condense the water vapor produced in the at least one reaction chamber, wherein the cooling chamber is configured to have an operating temperature of less than or equal to about 50° C.2. The reactor of claim 1 , wherein the at least one reaction chamber is configured to produce the solid carbon material through at least one of a Bosch reaction claim 1 , a Boudouard reaction claim 1 , and a methane reduction reaction.3. The reactor of claim 1 , wherein the at least one reaction chamber is configured to withstand an operating temperature greater than or equal to about 450° C.4. (canceled)5. (canceled)6. The reactor of claim 1 , further comprising a heat exchange zone operatively associated each of at least one effluent gas line and at least one return gas line extending between the at least one reaction chamber and the at least one cooling chamber claim 1 , and configured to exchange heat between the at least one effluent gas line and the at least one return gas line.7. The reactor of claim 1 , further comprising at least one prime mover operatively associated with each of the at least ...

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Номер записи: 98
06-10-2016 дата публикации

METHOD OF PREHEATING DEHYDROGENATION REACTOR FEED

Номер: US20160288079A1
Автор: Oleksy Slawomir A.
Принадлежит:

Methods and systems for heating a reactor feed in a multi reactor hydrocarbon dehydrogenation process. The methods and systems are advantageously employed for the production of styrene by the catalytic dehydrogenation of ethylbenzene. The catalytic dehydrogenation process employs heating steam operating at a steam to oil ratio of about 1.0 or less and relatively low steam superheater furnace temperature, such that all components exposed to steam in the process (outside of the fired heaters) can be constructed with standard metallurgy. 1. A method of heating a reactor feed in a multi reactor hydrocarbon dehydrogenation process comprising the steps of:(i) heating a first reheating steam stream against flue gas from one or more fired heaters, after the reheating steam stream heats a first reactor product stream in one or more first reactor product stream indirect heating apparatuses, to provide a preheating steam stream;(ii) heating a first reactor feed stream comprising a hydrocarbon and optionally feed steam, with the preheating steam stream in a first reactor feed stream indirect heating apparatus prior to entering a first reactor, to provide a preheated hydrocarbon stream and a cooled preheating steam stream;(iii) heating the cooled preheating steam stream in one of the one or more fired heaters to provide a second reheating steam stream;(iv) directing the second reheating steam stream to one of the one or more first reactor product stream indirect heating apparatuses to provide heat to the first reactor product stream and a cooled reheating steam stream;(v) heating the cooled reheating steam in one of the one or more fired heater to provide a heating steam stream; and(vi) mixing the heating steam stream with the preheated hydrocarbon stream prior to entering the first reactor.2. The method of claim 1 , wherein the first reactor product stream indirect heating apparatuses are arranged in series with respect to the first reactor product stream.3. The method of claim ...

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Номер записи: 99
05-10-2017 дата публикации

Treatment of Heavy Crude Oil and Diluent

Номер: US20170282148A1
Автор: Gieskes Thomas, Jarlsjo Bengt Arne, McCarver Lance Dawson, Moore Joe Travis
Принадлежит:

An integrated process simultaneously removes the diluent and reduces the TAN, resulting in cost savings from the diluent recovery and increasing the value of the produced heavy crude stream by removing the acids and other contaminants, while reducing the overall energy requirements when compared to performing the two processes separately. 1. An apparatus comprising:one or more heaters to heat a blend of bituminous crude oil and diluent to degradation of naphthenic acids in the crude oil;one or more reactors to provide sufficient residence time at elevated temperatures for the decomposition reactions to reduce the acid concentrations to reduce total acid number by at least 75% and to simultaneously remove the diluent; anda distillation column to remove diluent by distillation.2. The apparatus of including: ["each reactor's vapor flow is individually controlled to maintain a constant rate over the required residence time; and", 'both liquid and vapor flow concurrently upwards in the reactor so that as more degradation products are formed, vapor flow is also increasing, while vapor and liquid are separated at the top of each reactor; and, 'multiple reactors, arranged such thatheaters between the reactors to compensate for the heat required for the vaporization of the light hydrocarbons.3. The apparatus of including a vertical concurrent upward flow path for both the bituminous oil blend and the evaporated diluents and a flow path for hydrocarbon vapor stream through the liquid to remove decomposition products and drive the reaction to completion.4. The apparatus of including a condenser to recover the light hydrocarbons from the vented vapors by cooling and condensing said vapors while venting the non-condensable contaminants and residual hydrocarbon vapors to a vapor destruction device.5. The apparatus of including said distillation column to recover from said light hydrocarbons the fractions in the distillate boiling range claim 1 , that were stripped with the ...

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Номер записи: 100