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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 3155. Отображено 100.
22-11-2012 дата публикации

Process for alkylation of toluene to form styrene and ethylbenzene

Номер: US20120296136A1
Автор: Sivadinarayana Chinta
Принадлежит: Fina Technology Inc

A process is disclosed for making styrene and/or ethylbenzene by reacting toluene with a C 1 source over a catalyst in at least one radial reactor to form a product stream comprising styrene and/or ethylbenzene.

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Номер записи: 1
14-03-2013 дата публикации

Method and device for the metered addition of fluids into reaction vessels

Номер: US20130064738A1
Автор: Andreas MÄCHLER, Christine Schnetz, Fritz Bircher, Manfred Schär, Philipp Haslebacher, Stefan Berger
Принадлежит: RESEACHEM GmbH

Proposed is a metering device ( 87, 54 ) for introducing a fluid ( 31 ) into a reaction vessel such as, for example, a bioreactor ( 2 ). The metering device according to the disclosure comprises a closure element ( 89 ) for closing the reaction vessel, at least one drop generator ( 33 ) arranged in the closure element, and a feed line ( 91 ) serving for feeding the fluid to the at least one drop generator. The drop generator comprises a nozzle ( 36 ) for dispensing the fluid into the reaction vessel, and a valve ( 35 ). In the closed state, the valve disconnects the nozzle from the feed line. The drop generator is suitable for generating individual drops of the fluid.

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Номер записи: 2
23-01-2014 дата публикации

Process for the production of hexamethlenediamine

Номер: US20140024859A1
Автор: Alberto Corona, Luciano Guida, Stefano Alini, Tommaso Crippa
Принадлежит: Radici Chimica SpA

It is described a process for the production of hexamethylenediamine by hydrogenation of adiponitrile, comprising an improved step of regeneration of the catalyst. Also described are an equipment for the production of hexamethylenediamine, and a washing apparatus ( 14 ) for implementing the catalyst regeneration step.

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Номер записи: 3
06-03-2014 дата публикации

Fluid treatment apparatus

Номер: US20140061027A1
Автор: Graham Tyrie, Neil Polwart, Steve Barfield
Принадлежит: Albagaia Ltd

A fluid treatment apparatus comprising: a reactor vessel defining a chamber and having an inlet and an outlet to allow fluid to flow through the chamber; a UV light source adapted to transmit light within the chamber; and a plurality of catalyst members comprising a catalytic outer surface, the catalyst members being freely contained within the chamber, wherein the apparatus is adapted to cause the catalyst members to move around within the chamber as fluid flows through the chamber.

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Номер записи: 4
05-01-2017 дата публикации

Systems and methods for producing propylene

Номер: US20170001928A1
Автор: AQIL Jamal, Sohel Shaikh, Zhonglin Zhang
Принадлежит: Saudi Arabian Oil Co

According to one or more embodiments described herein, a process for producing propylene, the process comprising at least partially metathesizing a first portion of a first stream to form a first metathesis-reaction product, at least partially cracking the first metathesis-reaction product to form a cracking-reaction product, the cracking reaction product comprising propylene and ethylene, at least partially separating ethylene from at least the cracking reaction product to form a first recycle stream, combining the first recycle stream with a second portion of the first stream to a form a mixed stream, and at least partially metathesizing the mixed stream to from a second metathesis-reaction product. In embodiments, the second metathesis-reaction product may comprise propylene, the first stream may comprise butene, and the first recycle stream may comprise ethylene.

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Номер записи: 5
04-01-2018 дата публикации

CONTINUOUS PROCESS FOR PREPARING ETHYLENE GLYCOL FROM A CARBOHYDRATE SOURCE

Номер: US20180002259A1
Автор: Gruter Gerardus Johannes Maria, van der Waal Jan Cornelis
Принадлежит:

Ethylene glycol is prepared from a carbohydrate source by reaction of the carbohydrate source with hydrogen in a continuous process, 1. Continuous process for preparing ethylene glycol from a carbohydrate source by reaction of the carbohydrate source with hydrogen ,wherein hydrogen, the carbohydrate source and a liquid diluent are continuously fed into a continuous stirred tank reactor wherein a catalyst system is present, which catalyst system comprises a tungsten compound and at least one hydrogenolysis metal selected from the groups 8, 9 or 10 of the Periodic Table of the Elements, to achieve the reaction between the carbohydrate source and hydrogen to ethylene glycol;wherein continuously a product mixture comprising ethylene glycol and diluent is removed from the continuous stirred tank reactor; andwherein continuously or periodically further at least a tungsten compound is added to the continuous stirred tank reactor (CSTR).2. Continuous process according to claim 1 , wherein the amount of tungsten added to the CSTR is such that the concentration thereof in the CSTR is substantially constant.3. Continuous process according to claim 1 , wherein the weight ratio of tungsten to the at least one hydrogenolysis metal claim 1 , all calculated as metals claim 1 , in the CSTR is in the range of 2 to 50 wt/wt.4. Continuous process according to claim 1 , wherein the weight ratio of tungsten calculated as metal to carbohydrate source in the CSTR is in the range of 5 to 50 wt/wt.5. Continuous process according to claim 1 , wherein the tungsten compound that is continuously or periodically added to the CSTR has an oxidation state of at least +2.6. Continuous process according to claim 1 , wherein the weight ratio of the at least one hydrogenolysis metal and carbohydrate that is introduced into the CSTR is in the range of 1:25 to 1:250 wt/wt.7. Continuous process according to claim 1 , wherein the tungsten compound that is continuously or periodically added to the CSTR claim ...

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Номер записи: 6
03-01-2019 дата публикации

PROCESS FOR THE PRODUCTION OF THERMALLY MODIFIED STARCH

Номер: US20190002593A1
Автор: Vezzani Massimo
Принадлежит: Ambiente E Nutrizione S.R.L.

Process for the production of thermally modified starch comprising the steps of mixing starch in powder form having a specific moisture content with an alkaline water solution to obtain a wet powder; feeding a continuous flow of said wet powder into a continuous dryer together with a continuous flow of hot air; discharging a continuous flow of dried powder from said continuous drier; supplying said continuous flow of said dried powder into a turbo-reactor, in which the inner wall of said turbo-reactor is maintained at a specific temperature; converting said dried powder into a thermally inhibited starch; and discharging said thermally inhibited starch from said turbo-reactor; it is also disclosed a thermally inhibited starch obtained from the aforementioned process with enhanced physical chemical properties. 1. A process for continuous modification of starch , comprising the steps of:a) mixing starch in powder form having a moisture content between 9% and 25% with an alkaline water solution to obtain a wet powder;b) feeding a continuous flow of said wet powder into a continuous dryer together with a continuous flow of hot air, said flow of hot air having a temperature between 100° C. and 160° C.;c) discharging a continuous flow of dried powder from said continuous drier, said dried powder having a moisture content between 2% and 4%;d) providing a turbo-reactor comprising a cylindrical tubular body having at least one inlet opening for the introduction of said continuous flow of dried powder and at least one discharge opening, a heating jacket for bringing the temperature of said tubular body to a predetermined temperature and a rotor, disposed in the cylindrical tubular body and comprising a shaft provided with elements projecting radially from it;e) supplying said continuous flow of said dried powder into said turbo-reactor, in which the inner wall of said turbo-reactor is maintained at a temperature between 150° C. and 250° C. by means of said heating jacket and ...

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Номер записи: 7
12-01-2017 дата публикации

METHOD FOR CONTINUOUSLY PRODUCING KETOMALONIC ACID COMPOUND USING FLOW REACTOR

Номер: US20170008829A1
Автор: Tani Shinki
Принадлежит: Ihara Chemical Industry Co., Ltd.

The purpose of the present invention is to provide a method for continuously producing a ketomalonic acid compound such as a ketomalonic acid diester or a hydrate thereof, which is an industrially useful compound, on an industrial scale and in a safe and steady manner. The present invention relates to: a method in which a malonic acid diester, a carboxylic acid compound and a chlorous acid compound are used as raw material compounds, and these raw material compounds are mixed together to prepare a mixture and the mixture is supplied to a flow reactor continuously, thereby continuously producing a corresponding ketomalonic acid diester or a hydrate thereof; and a continuous production apparatus for performing the method. 2. The method according to claim 1 , wherein the chlorous acid compound is supplied as an aqueous solution of a chlorous acid compound.3. The method according to claim 1 , wherein the malonic acid diester or a mixture of the malonic acid diester and the carboxylic acid compound is supplied in the absence of a solvent.4. The method according to claim 1 , wherein the flow reactor(s) are one or two or more tubular flow reactors.5. The method according to claim 1 , wherein the flow reactor(s) are provided with a temperature control part configured to control a temperature.6. The method according to claim 5 , wherein the temperature control part provided to the flow reactor(s) is a bath and a temperature of the bath is 80° C. or higher.7. The method according to claim 1 , wherein the method comprising:(D) a process of further aging the reaction mixture obtained in the process of reacting the mixture in addition to the processes of said (A) to (C).8. The method according to claim 7 , wherein the aging process (D) is performed in one or two or more second flow reactors.9. The method according to claim 1 , wherein the method comprising:(E) a process of quenching the reaction by mixing a quench liquid in addition to the processes of said (A) to (C) or the ...

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Номер записи: 8
17-01-2019 дата публикации

UREA PRODUCTION WITH BI-PRESSURIZED SYNTHESIS

Номер: US20190015811A1
Автор: COLOMA GONZÁLEZ Juan, Dieltjens Luc Louis Maria, Mennen Johannes Henricus
Принадлежит: Stamicarbon B.V.

Disclosed is a urea plant wherein, in deviation from conventional plants, a high-pressure synthesis section is operated with two different pressures. The synthesis section comprises a reactor, which is operated under a first high pressure. The synthesis section also comprises a stripper and a condenser, both operated at substantially the same second high pressure. In accordance with the invention, the first pressure is substantially higher than the second pressure. The disclosed plant particularly comprises a compression unit capable of converting a pressure difference into work, or more specifically, mechanical energy for compression. This compression unit is positioned between a liquid outlet of the condenser and a liquid inlet of the reactor, and in fluid communication therewith. In order to make use of a pressure drop (expansion as a result of a liquid being depressurized), said compression unit is configured to obtain compression energy from one or more events in the urea production process (i.e., at one or more points in the urea production plant), at which a loss of energy occurs, such as decompression of a high energy stream. Typically, the compression unit is thereby configured to utilize mechanical energy recovered from a decompression unit positioned downstream of the stripper and upstream of the recovery section. 1. A plant for the production of urea comprising a synthesis section configured to be operated under a high pressure between 12 and 40 MPa and a recovery section configured to be operated under a pressure below 7 MPa , said synthesis section comprising , connected so as to be capable of forming a urea synthesis loop , a urea reactor , a stripper , a condenser and , optionally , a scrubber , wherein the synthesis section is configured so as to allow the reactor to be operated under a pressure substantially higher than the pressure of the stripper and the condenser , and wherein the synthesis section comprises a compression unit positioned ...

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Номер записи: 9
17-01-2019 дата публикации

Process of Removing Heat

Номер: US20190016654A1
Автор: Andre Peter Steynberg, Dennis Parker, Ivan Phillip GREAGER, Jasmeer Jaichland RAMLAL, John Dolan, Roger Allen HARRIS, Steven Claude Leviness
Принадлежит: Velocys Inc, Velocys Technologies Ltd, VENTECH ENGINEERS INTERNATIONAL LLC

The present invention provides an improved process for removing heat from an exothermic reaction. In particular, the present invention provides a process wherein heat can be removed from multiple reaction trains using a common coolant system.

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Номер записи: 10
21-01-2021 дата публикации

FLOW TYPE REACTION DEVICE

Номер: US20210016242A1
Автор: Sakai Kazuya, TOKUOKA Shinya
Принадлежит:

An object of the present invention is to provide a flow type reaction device which is capable of maintaining reaction efficiency and productivity which are sufficient for practical use for a long time, and reducing the size and cost of the reaction device, and the present invention provides a flow type reaction device () for continuously reacting two or more kinds of raw materials, including a mixing section () which is configured to mix two or more kinds of the raw materials, and a reaction section () which is provided on a secondary side with respect to the mixing section (), and configured to obtain a product by reacting two or more kinds of the raw materials, the mixing section () includes a mixing device () which is configured to mix two or more kinds of the raw materials, and two or more supply pipes (L, L) which are configured to supply each of two or more kinds of the raw materials to the mixing device (), the supply pipes (L, L) are respectively connected to the mixing device (), and at least one of the supply pipes (L) has, in the vicinity of a connection portion of the supply pipe (L) with the mixing device (), a suppression mechanism which is configured to suppress movement of a fluid from the mixing device () to the supply pipe (L). 1. A flow type reaction device for continuously reacting two or more kinds of raw materials ,wherein the flow type reaction device includes a mixing section which is configured to mix two or more kinds of the raw materials, and a reaction section which is provided on a secondary side with respect to the mixing section, and configured to obtain a product by reacting two or more kinds of the raw materials,the mixing section includes a mixing device which is configured to mix two or more kinds of the raw materials, and two or more supply pipes which are configured to supply each of two or more kinds of the raw materials to the mixing device,the supply pipes are respectively connected to the mixing device, and at least one of ...

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Номер записи: 11
21-01-2021 дата публикации

PROCESS FOR PRODUCING METHANOL AND AMMONIA

Номер: US20210017023A1
Автор: Ingham Alan, Janardhanan Madhanakrishnan, PACH John David, Yiu Kar Chi
Принадлежит:

A process for the co-production of methanol and ammonia is described comprising the steps of: (a) forming a first synthesis gas stream by reacting a first portion of a hydrocarbon feedstock and steam in a steam reformer, (b) forming a second synthesis gas stream in parallel to the first synthesis gas stream by reacting a second portion of the hydrocarbon feedstock with an oxygen-containing gas and steam in an autothermal reformer, (c) synthesising methanol from a first process gas comprising the first synthesis gas stream, and (d) synthesising ammonia from a second process gas prepared from the second synthesis gas stream, wherein a purge stream containing hydrogen is recovered from the methanol synthesis step (c) and a portion of the purge gas stream is fed to the autothermal reformer and/or the second synthesis gas in step (b). 1. A process for the co-production of methanol and ammonia comprising the steps of: (a) forming a first synthesis gas stream by reacting a first portion of a hydrocarbon feedstock and steam in a steam reformer , (b) forming a second synthesis gas stream in parallel to the first synthesis gas stream by reacting a second portion of the hydrocarbon feedstock with an oxygen-containing gas and steam in an autothermal reformer , (c) synthesising methanol from a first process gas comprising the first synthesis gas stream , and (d) synthesising ammonia from a second process gas prepared from the second synthesis gas stream , wherein a purge stream containing hydrogen is recovered from the methanol synthesis step (c) and a portion of the purge gas stream is fed to the autothermal reformer and/or the second synthesis gas in step (b).2. A process according to wherein the purge gas stream containing hydrogen is separated into a hydrogen-rich gas stream and a hydrogen-depleted gas stream and the hydrogen-rich gas stream is combined with the second synthesis gas stream.3. A process according to wherein the hydrogen-depleted gas is fed to the autothermal ...

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Номер записи: 12
21-01-2021 дата публикации

A PROCESS FOR MAKING BROMINATING AGENTS IN FLOW

Номер: US20210017024A1
Автор: CAPPUYNS Bart, DERMAUT Wim, MOENS Matthias, Stevens Christian
Принадлежит:

A process for making a brominating agent includes the step of continuously feeding a bromide source and an oxidizing agent into a continuous flow reactor. 110-. (canceled)11. A process for making a brominating agent comprising:continuously feeding a bromide source and an oxidizing agent into a continuous flow reactor; whereinthe oxidizing agent is selected from the group consisting of a hypochlorite anion, nitric acid, oxygen, osmium tetroxide, chlorine, fluorine, ozone, peracids, potassium permanganate, and potassium peroxymonosulfate.12. The process according to claim 11 , wherein the bromide source is selected from the group consisting of hydrogen bromide and an organic or inorganic bromide salt.13. The process according to claim 11 , wherein the bromide source is selected from the group consisting of an alkali metal bromide salt claim 11 , an earth alkali metal bromide salt claim 11 , and an ammonium bromide salt.14. The process according to claim 11 , wherein the bromide source is an alkali metal bromide salt.15. The process according to claim 12 , wherein the bromide source is an alkali metal bromide salt.16. The process according to claim 11 , wherein the oxidizing agent has a standard reduction potential claim 11 , with respect to a potential of a standard hydrogen electrode claim 11 , greater than 0.5 V.17. The process according to claim 12 , wherein the oxidizing agent has a standard reduction potential claim 12 , with respect to a potential of a standard hydrogen electrode claim 12 , greater than 0.5 V.18. The process according to claim 14 , wherein the oxidizing agent has a standard reduction potential claim 14 , with respect to a potential of a standard hydrogen electrode claim 14 , greater than 0.5 V.19. The process according to claim 11 , wherein the oxidizing agent is a hypochlorite anion.20. The process according to claim 12 , wherein the oxidizing agent is a hypochlorite anion.21. The process according to claim 14 , wherein the oxidizing agent is a ...

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Номер записи: 13
21-01-2021 дата публикации

Oligomerization Reactor Wash Process Using By-Product Solvent Recovered Using a Thin Film Evaporator

Номер: US20210017104A1
Автор: Coleman John S., Iaccino Larry L., Kuechler Keith H., Reimers Jay L., Weber Michael W.
Принадлежит:

A method for washing an oligomerization reactor using by-product solvent recovered from the reactor can include: catalytically converting a monomer in a reactor section in a reaction mode in the presence of a catalyst to form a product stream comprising an oligomer, a by-product solvent, and a polymeric by-product; separating the product stream into a first fraction comprising the oligomer and a second fraction comprising a mixture of the by-product solvent and the polymeric by-product; and separating, in a thin film evaporator, the second fraction into a third fraction comprising the by-product solvent and a fourth fraction comprising the polymeric by-product. 1. A method comprising:catalytically converting a monomer in a reactor section in a reaction mode in the presence of a catalyst to form a product stream comprising an oligomer, a by-product solvent, and a polymeric by-product;separating the product stream into a first fraction comprising the oligomer and a second fraction comprising a mixture of the by-product solvent and the polymeric by-product; andseparating, in a thin film evaporator, the second fraction into a third fraction comprising the by-product solvent and a fourth fraction comprising the polymeric by-product.2. The method of claim 1 , further comprising delivering a recycled portion of the by-product solvent to the reactor section in a wash mode; wherein the recycled portion of the by-product solvent comprises the third fraction.3. The method of claim 1 , wherein the product stream claim 1 , the second fraction claim 1 , and the fourth fraction each further comprise at least a portion of the catalyst.4. The method of claim 1 , further comprising:delivering the recycled portion of the by-product solvent to a collection vessel in the reaction mode; anddelivering the recycled portion of the by-product from the collection vessel to the reactor section in the wash mode.5. The method of claim 1 , wherein the first fraction comprises further comprises ...

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Номер записи: 14
22-01-2015 дата публикации

Ozonization continuous reaction device and a working method thereof

Номер: US20150021279A1
Автор: Furong CHEN, Hao Hong, Jian Tao
Принадлежит: Individual

The invention discloses an ozonization continuous reaction device, comprising a raw material inlet, a raw material distributing device, one or plurality of single reaction tubes, a product outlet and an air vent. The first end of the raw material distributing device is communicated with the raw material inlet; the first end of one or plurality of single reaction tubes is communicated with the second end of the raw material distributing device; the product outlet is communicated with the second end of the single reaction tube; ozone is conveyed to the single reaction tube via the air vent. The ozonization continuous reaction device provided by the invention realizes the large-scale and continuous production of the ozonization reaction on the basis of guaranteeing security; as the single reaction tube is arranged, the ozone amount and the liquid raw material existing in the single reaction tube in unit time become fewer, the reaction security is greatly improved; in addition, the liquid raw material and the ozone are continuously fed into the reaction device, the exhaust gas and the products are continuously discharged from the reaction device, the accumulation of the ozone is prevented, the security is greatly guaranteed, and the production capacity also can be improved to a higher level.

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Номер записи: 15
26-01-2017 дата публикации

SERPENTINE FLUID REACTOR COMPONENTS

Номер: US20170022427A1
Автор: Benum Leslie Wilfred, Clavelle Eric, Eisenhawer David, Foy Edward Christopher, Yajure Edgar
Принадлежит: NOVA CHEMICALS (INTERNATIONAL) S.A.

Some embodiments of the present invention provide components for a serpentine fluid reactor which is optimized for one or more objective functions of interest such as pressure drop, erosion rate, fouling, coke deposition and operating costs. The components are designed by computer modeling the components individually and collectively in which the cross section of flow path is substantially circular under industrial conditions to validate the model design and its operation. Then iteratively the component designs are deformed and the operation of the deformed part(s) is modeled and compared to values obtained with other deformed models until the value of the objective function is optimized (e.g. at an extreme) or the change in the objective function is approaching zero. 2. The method according to claim 1 , wherein the first pipe sections are part of a high pressure olefin polymerization reactor wherein the hydrocarbon comprises ethane.3. The method according to claim 1 , wherein the first pipe section is part of the furnace tubes of an olefin cracker.4. The method according to claim 3 , wherein over 90% of the flow passage does not change by more than 7% over an about 5% length of the flow path.5. The method according to claim 4 , wherein the ARQ at one or more sections over said 90% of the length of the flow passage is from about 1.02 and about 1.12.6. The method according to claim 5 , wherein the ARQ over said 80% of the length of the flow passage does not change by more than about 5% over an about 5% length of the flow path.722-. (canceled)23. The method according to claim 6 , wherein the ARQ at one or more sections over said remaining about 80% of the length of the flow passage is from about 1.02 and about 1.15.24. The method according to claim 23 , wherein the serpentine reactor has an increasing cross sectional area in the direction of flow such that the angle between the transverse normal vector and the pipe walls range from about 0° to about 85°.25. The method ...

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Номер записи: 16
01-02-2018 дата публикации

APPARATUS AND METHOD FOR CONTINUOUS PRODUCTION OF POLYETHYLENE GLYCOL DINITRATE

Номер: US20180029004A1
Автор: JENNINGS James Robert, SHORT Glyn David
Принадлежит:

An apparatus for producing polyethylene glycol dinitrate. The apparatus includes providing continuously an acid composition and a glycol composition to a reaction apparatus; reacting the acid composition and the glycol composition in the reaction apparatus in a continuous manner to generate a reaction composition; using an alkaline composition to at least partially neutralize the reaction composition to cause at least a portion of the polyethylene glycol dinitrate to deposit from a solution of the reaction composition; and extracting the deposit of polyethylene glycol dinitrate. 113-. (canceled)14. A reaction apparatus for producing in a continuous manner polyethylene glycol dinitrate (PEGDN) , characterized in that the reaction apparatus includesa series of reaction cells spatially disposed in one or more planar structures, the plurality of reaction cells constitute;a feed preparation section having feedstreams for continuously providing an acid composition and a glycol composition to reaction cells thereof, wherein the acid composition includes a mixture of dilute nitric acid and concentrated sulphuric acid;a nitration section in which the acid composition and the glycol composition react in reaction cells in a continuous manner to generate a reaction composition;a quench and neutralization section having a feed for a cooling arrangement for cooling reaction cells to avoid spatial reaction hotspots and thereby preventing thermal runaway occurring within the reaction apparatus, and a plurality of feeds for providing an alkaline composition to at least partially neutralize the reaction composition to cause at least a portion of the polyethylene glycol dinitrate to deposit from a solution of the reaction composition; anda separation arrangement for extracting the deposit of polyethylene glycol dinitrate.15. The reaction apparatus of claim 14 , characterized in that the dilute nitric acid has a concentration in a range of 50-70 weight %.16. The reaction apparatus of ...

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Номер записи: 17
04-02-2021 дата публикации

CONTINUOUS PROCESS FOR THE PREPARATION OF TRAZODONE

Номер: US20210032243A1
Автор: Caracciolo Torchiarolo Giuliano, CAVARISCHIA Claudia, FURLOTTI Guido, Iacoangeli Tommaso, MORO Leonardo Mario
Принадлежит: AZIENDE CHIMICHE RIUNITE ANGELINI FRANCESCO A.C.R.A.F. S.p.A.

The present invention relates to an improved process for the preparation of trazodone. In particular, the present invention relates to a continuous process for the preparation of trazodone. More in particular, the present invention relates to a new method for the preparation of trazodone, said method comprising at least one step consisting of a continuous process performed in a flow reactor. 2: The continuous process according to claim 1 , comprising:(i) continuously feeding a first channel of a flow reactor with an aqueous solution of s-triazolo-[4,3-a]-pyridin-3-one (III) and at least one basic compound;(ii) continuously feeding a second channel of said flow reactor with an organic solution of N-(3-chlorophenyl)-N′-(3-chloropropyl)-piperazine (II) in at least one organic solvent;(iii) continuously reacting said s-triazolo-[4,3-a]-pyridin-3-one (III) with said N-(3-chlorophenyl)-N′-(3-chloropropyl)-piperazine (II) by continuously mixing said alkaline aqueous solution and said organic solution in said flow reactor, at a temperature of at least 90° C.; and(iv) continuously collecting said reaction mixture from said flow reactor, and isolating the obtained product trazodone base (IV).3: The process according to claim 1 , wherein trazodone base (IV) is obtained with a conversion yield of at least 70% by HPLC.4: The process according to claim 1 , wherein trazodone base (IV) has a purity of at least 90% by HPLC.5. (canceled)6: The process according to claim 2 , wherein the temperature of said continuously reacting iii) is from 130° C. to 160° C.7: The process according to claim 2 , wherein said basic compound in said continuously feeding a first channel i) is an inorganic base selected from the group consisting of sodium hydroxide claim 2 , potassium hydroxide claim 2 , sodium hydride claim 2 , sodium amide claim 2 , sodium carbonate claim 2 , potassium carbonate claim 2 , sodium bicarbonate claim 2 , potassium bicarbonate claim 2 , sodium phosphate claim 2 , potassium ...

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Номер записи: 18
05-02-2015 дата публикации

Process for preparing polymers and reactor for performing the process

Номер: US20150038656A1
Автор: ABBOUD Mohammed, Desbois Philippe, Gmaehle Norbert, Krebs Thilo, Lösch Dennis, Roemer Herbert
Принадлежит:

The invention relates to a process for preparing polymers from monomers and/or oligomers by adding a liquid comprising the monomers and/or oligomers dropwise to a continuous liquid phase in a reactor, the continuous liquid phase being immiscible with the liquid comprising the monomers and/or oligomers, and the monomers and/or oligomers reacting in the continuous liquid phase to give the polymer. The liquid comprising the monomers and/or oligomers is shaped to droplets outside the continuous liquid phase, which are subsequently introduced into the continuous liquid phase. The invention further relates to a reactor for performing the process, comprising a tube through which a continuous liquid phase flows, and means of generating droplets, the means of generating droplets being arranged such that the droplets are generated outside the continuous liquid phase and then introduced into the continuous liquid phase. 1. A reactor comprising a tube through which a continuous liquid phase flows , and means of generating droplets , the means of generating droplets being arranged such that the droplets are generated outside the continuous liquid phase and then introduced into the continuous liquid phase ,wherein the reactor is used in a process for preparing polymers from monomers and/or oligomers comprising: adding a liquid comprising monomers and/or oligomers dropwise to a continuous liquid phase in a reactor, the continuous liquid phase being immiscible with the liquid comprising the monomers and/or oligomers, and the monomers and/or oligomers reacting in the continuous liquid phase to produce the polymer, which comprises shaping the liquid comprising the monomers and/or oligomers to droplets outside the continuous liquid phase and then introducing them into the continuous liquid phase.2. The reactor according to claim 1 , wherein the means of generating droplets are arranged above the continuous liquid phase claim 1 , such that the droplets fall from the means of generating ...

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Номер записи: 19
08-02-2018 дата публикации

Systems and processes for producing polyether polyols

Номер: US20180036704A1
Автор: D. Mark Morrison, Jack R. Reese, Jye-Sheng Lai, Robert A. Lenahan, William D. Wray
Принадлежит: Covestro LLC

Disclosed are processes and systems for producing polyether polyols and for the recovery of heat generated during such polyether polyol production.

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Номер записи: 20
07-02-2019 дата публикации

ENHANCED EFFICIENCY ENDOTHERMIC REACTOR FOR SYNGAS PRODUCTION WITH FLEXIBLE HEAT RECOVERY TO MEET LOW EXPORT STEAM GENERATION

Номер: US20190039038A1
Автор: Guazzotti Cristina, Mosca Lorena, PALO Emma
Принадлежит:

An apparatus for carrying out endothermic reactions including a plurality of catalytic vessels, immersed in a combustion chamber having a contiguous overlaid convection chamber enclosing a top portion of the catalytic vessels wherein heat is recovered at a lower temperature level from the flue gases from the combustion chamber. The catalytic vessels may contain internal and coaxial heat recovery tubes creating an annular space filled in with a catalytic device. Both the external heat recovery through the catalyst tube outer surface and the internal heat recovery through the inner tube surface can be maximized by an enhanced catalytic device acting also as a heat transfer promoter in the process gas region. The apparatus provides enhanced and flexible heat recovery that permits to meet the request of minimum or none export steam production in one single apparatus, avoiding the need of a pre-reforming section and/or of a convective reformer downstream. 114-. (canceled)15. An apparatus for conducting endothermic reactions able to meet the heat balance with a null or limited amount of export steam , through a flexible heat recovery , comprising:a combustion chamber having a closed bottom end, an open top end, two opposite end walls, and two opposite side walls;an upper convection chamber, in communication with said combustion chamber through said open top end, allowing the flow of flue gas through a plurality of convection channels in flow communication with a top plenum chamber connected to an outlet flue gas channel;a plurality of catalytic vessels arranged at a distance and disposed in line or staggered along the centerline of the combustion and convection chamber in such a way that the bottom portion is immersed in the combustion chamber and the remaining top portion is immersed in the convection chamber wherein the portion of the catalytic vessel immersed in the combustion chamber is such that the flue gas temperature at its exit and inlet of the convection chamber ...

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Номер записи: 21
12-02-2015 дата публикации

METHOD FOR HYDROLYSING ACETONE CYANOHYDRIN

Номер: US20150045577A1
Автор: Deinken Joachim, Groemping Matthias, Gropp Udo, Mertz Thomas, Mnich Norbert, Perl Andreas, SARTORELLI Lorenza, Selbach Arndt, Sohnemann Stefanie
Принадлежит: Evonik Roehm GmbH

The present invention relates to a process for hydrolysis of acetone cyanohydrin (ACH) by means of sulphuric acid within the ACH sulpho process for preparation of methacrylic acid (MAA) or methyl methacrylate (MMA). 1. A process for hydrolysis of acetocyanohydrin , the process comprising:preparing methyl methacrylate in a loop reactor by using sulphuric acid as a precursor,whereinat least one heat exchanger present in the loop reactor is equipped with turbulators,at least one reaction component is fed into the loop reactor via a metering ring, which is installed externally and immediately upstream of a pump with a pump housing in the loop reactor, andthe at least one heat exchanger equipped with turbulators is positioned downstream of a metered addition of sulphuric acid and of acetocyanohydrin in flow direction.2. (canceled)3. The process according to claim 1 , wherein the metering ring is integrated into the pump housing.4. The process according to claim 1 , wherein corkscrew-like or pipebrush-like structures are installed as turbulators into the at least one heat exchanger.5. The process according to claim 1 , wherein various kinds of structures are used on turbulators in the loop reactor.6. The process according to claim 1 , wherein the at least one heat exchanger is a modified shell-and-tube heat exchanger claim 1 , and at least 50-70% of tubes of the modified shell-and-tube heat exchanger are equipped with turbulators.7. The process according to claim 1 , wherein the turbulators are turbulators with 500-750 turns/m. The present invention relates to a process for hydrolysis of acetone cyanohydrin (ACH) by means of sulphuric acid within the ACH sulpho process for preparation of methacrylic acid (MAA) or methyl methacrylate (MMA).The preparation of MAA or MMA by the ACH sulpho process is common knowledge and is described, for example, in EP 2054370. Proceeding from hydrogen cyanide and acetone, ACH is prepared in a first step, and is then converted to ...

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Номер записи: 22
15-02-2018 дата публикации

Systems and Methods for the Continuous On-Site Production of Peroxycarboxcylic Acid Solutions

Номер: US20180042231A1
Автор: Anderson David H, Del Negro Andrew S., Grimmer Paul, Riffell Daniel J
Принадлежит: Eltron Water Systems, LLC

Methods and systems for on-site production of peroxycarboxcylic acid compositions, and in particular, nonequilibrium compositions of peracetic acid (PAA) enable the economical and safe production of PAA on-demand at the point of use. The methods and systems control flow rates and proportions of feedstocks/reactants, perform the required sequence of reaction steps to produce high yield peroxycarboxcylic acid solutions in a continuous manner, and provide optimal reaction time and reactant mixing for continuous and safe on-site production. 1. A method for the continuous production of non-equilibrium peracetic acid solutions containing biocidal concentrations of peroxycarboxylic acids , the method comprising:providing a source of hydrogen peroxide having an initial pH of less than 7.0;diluting the hydrogen peroxide with water to create a diluted solution having a concentration which is less than 10% weight/volume;adding an alkali metal hydroxide to the diluted solution to adjust the pH to a pH in a range of approximately 10.0 to approximately 13.5;reacting the diluted solution with an O-acetyl or N-acetyl donor;vigorously mixing the solution.2. The method of further including the step of controlling the stoichiometry of the peroxide component with respect to the acetyl donor to bias the reaction in favor of either producing peracetic acid or producing a solution having a specified remaining concentration of peroxide.3. The method of wherein the alkali metal hydroxide is sodium hydroxide.4. The method of wherein the alkali metal hydroxide is potassium hydroxide.5. The method of wherein the O-acetyl donor is triacetin.6. The method of wherein the step of mixing the solution includes producing a turbulent flow having high shear within the solution and having a Reynolds number of 500 or greater.7. The method of including the step of vigorously mixing the solution following the diluting step.8. The method of further including the step of vigorously mixing the solution ...

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Номер записи: 23
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: 24
24-02-2022 дата публикации

RUNNING MULTIPLE EXPERIMENTS SIMULTANEOUSLY ON AN ARRAY OF CHEMICAL REACTORS

Номер: US20220059192A1
Автор: Geluykens Joppe, Georgopoulos Leonidas, Harikrishnan Nair Vishnu, Laino Teodoro, Schwaller Philippe, Sobczyk Aleksandros, Vaucher Alain Claude
Принадлежит:

A method for executing multiple chemical experiments in parallel may be provided. The method comprises receiving a list of actions to be performed for synthesizing a chemical product. Thereby, the actions correspond to at least two chemical partial reactions and the list comprises a delimiter symbol separating two chemical partial reactions, determining identical chemical partial reactions, and building a reaction commonality tree (RCT) of the chemical reactions. Furthermore, the method comprises executing a plurality of the identical chemical partial reactions independent of a sequence of chemical partial reactions of the reaction commonality tree only once. Each of the identical chemical partial reactions is executed in a different chemical reactor and each resulting intermediate product has a quantity of the sum of the related identical chemical partial reactions. The method also comprises, storing the intermediate chemical products in a separate container, and executing remaining chemical partial reactions according to the RCT. 1. A method for executing multiple chemical experiments in parallel on an array of chemical reactors , the method comprising:receiving a list of actions to be performed for synthesizing a chemical product, wherein the list of actions corresponds to at least two chemical partial reactions, wherein the list comprises a delimiter symbol separating each of the at least two chemical partial reactions in the list of actions;determining identical chemical partial reactions in the list of actions;building a reaction commonality tree of the chemical partial reactions according to subsequent points in time in the list of actions executing a plurality of the identical chemical partial reactions independent of a sequence of chemical partial reactions of the reaction commonality tree only once, wherein each of the plurality of identical chemical partial reactions is executed in a different reactor of the array of chemical reactors, wherein each ...

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Номер записи: 25
16-02-2017 дата публикации

METHOD FOR CONTINUOUSLY PREPARING NANO ZINC OXIDE WITH MEMBRANE REACTOR

Номер: US20170044021A1
Автор: Xing Weihong, Xu Nanping, XU Zhilong, Zhang Feng, Zhong Zhaoxiang
Принадлежит:

The present invention relaters to a method for continuously preparing a nano zinc oxide with a membrane reactor. A zinc salt solution and a precipitator solution required for the preparation of a zinc oxide are respectively used as dispersion phases, and under the action of a certain pressure, the two reaction solutions respectively penetrate through a membrane tube at a certain rate and disperse quickly under the action of a shear force and react, producing a precursor precipitate. A precursor suspension penetrates through the membrane tube continuously and circularly after being pressurized by a pump, and at the same time, deionized water as a washing fluid is added to a suspension storage tank, wherein impurity ions penetrate through membrane pores and are discharged along with the liquid medium; after the concentration of the impurity ions meets requirements, the concentrated solution is discharged continuously and then spray-dried to obtain a basic zinc carbonate precursor powder. The basic zinc carbonate powder is calcined under certain conditions to obtain the nanostructured zinc oxide powder. The continuous preparation and washing of a powder can be achieved by coupling a membrane washing technique with a membrane dispersion technique. The procedure is simple, the structure of zinc oxide is easy to control and the yield is high. 1. A method for continuously preparing nano zinc oxide with membrane reactor; the specific steps are as follows: zinc salt solution and precipitator solution are put into the reactor membrane tube for dispersion via metering pump at a certain charging ratio and disperse to the reactor from membrane tube by stirring; with the temperature of reactor controlled , the dispersed droplets are uniformly mixed for nucleation and reaction in the reactor to produce suspension solution containing solid which is pumped from the reactor to the storage tank; the suspension solution containing solid inside the storage tank flows through the washing ...

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Номер записи: 26
19-02-2015 дата публикации

CONTINUOUS POLYMERIZATION APPARATUS AND PROCESS FOR PRODUCING POLYMER COMPOSITION

Номер: US20150051359A1
Автор: Sumida Masakazu, Yamazaki Kazuhiro
Принадлежит: Sumitomo Chemical Company, Limited

Continuous polymerization apparatus including a first reactor of a complete mixing type and a second reactor of a complete mixing type (). Each of the reactors () is provided with a supply port (), an effluent port (), and a temperature detecting means (T) for detecting a temperature in the reactor, wherein the supply port () of the first reactor () is connected to the supply sources () of a raw material monomer and a polymerization initiator, and the effluent port () of the first reactor is connected through a connection line () to the supply port () of the second reactor (). Connection line () is combined with a secondary line (′) for supplying a raw material monomer at a combining part (M) located between the effluent port () of the first reactor () and the supply port () of the second reactor (). 1. A continuous polymerization apparatus which comprises , at least , a first reactor and a second reactor which are of a complete mixing type ,wherein each of the reactors is provided with a supply port, an effluent port, and a temperature detecting means for detecting a temperature in the reactor,the supply port of the first reactor is connected to supply sources of a raw material monomer and a polymerization initiator,the effluent port of the first reactor is connected through a connection line to the supply port of the second reactor,the connection line is combined with a secondary line for supplying a raw material monomer at a combining part located between the effluent port of the first reactor and the supply port of the second reactor, andwherein the secondary line is connected to a source of the raw material monomer, and at least one of said source and said secondary line is provided with a temperature regulating means.2. (canceled)3. The continuous polymerization apparatus according to claim 1 , wherein the connection line is provided with a cooling means.4. The continuous polymerization apparatus according to claim 1 , wherein the connection line is provided ...

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Номер записи: 27
03-03-2022 дата публикации

REACTION SCHEMES INVOLVING ACIDS AND BASES; REACTORS COMPRISING SPATIALLY VARYING CHEMICAL COMPOSITION GRADIENTS; AND ASSOCIATED SYSTEMS AND METHODS

Номер: US20220064063A1
Автор: Badel Andres, CHIANG Yet-Ming, Ellis Leah
Принадлежит: Massachusetts Institute of Technology

Reaction schemes involving acids and bases; reactors comprising spatially varying chemical composition gradients (e.g., spatially varying pH gradients), and associated systems and methods, are generally described.

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Номер записи: 28
03-03-2022 дата публикации

METHODS AND SYSTEMS FOR PROCESSING CRUDE OIL

Номер: US20220064556A1
Автор: Akah Aaron Chi, Al-Ghrami Musaed Salem, XU QI
Принадлежит:

A feed stream including crude oil may be processed by a method that includes separating the feed stream into at least a Chydrocarbon fraction, a C-Chydrocarbon fraction, and a Chydrocarbon fraction. The method may further include methane cracking at least a portion of the Chydrocarbon fraction to form a methane cracked product, steam cracking at least a portion of the C-Chydrocarbon fraction to form a steam cracked product, and steam enhanced catalytically cracking at least a portion of the Chydrocarbon fraction to form a steam enhanced catalytically cracked product. The method may further include passing at least a portion of the steam cracked product and at least a portion of the steam enhanced catalytically cracked product to a product separator to produce one or more product streams. Systems for processing a feed stream comprising crude oil are further described herein. 1. A method for processing a feed stream comprising crude oil , the method comprising:{'sub': 1', '2', '4', '5+, 'separating the feed stream into at least a Chydrocarbon fraction, a C-Chydrocarbon fraction, and a Chydrocarbon fraction;'}{'sub': '1', 'methane cracking at least a portion of the Chydrocarbon fraction to form a methane cracked product comprising hydrogen;'}{'sub': 2', '4', '2', '4, 'steam cracking at least a portion of the CChydrocarbon fraction to form a steam cracked product comprising C-Colefins;'}{'sub': '5+', 'steam enhanced catalytically cracking at least a portion of the Chydrocarbon fraction to form a steam enhanced catalytically cracked product comprising olefins, benzene, toluene, xylene, naphtha, or combinations thereof; and'}passing at least a portion of the steam cracked product and at least a portion of the steam enhanced catalytically cracked product to a product separator to produce one or more product streams.2. The method of claim 1 , wherein the one or more product streams comprise:{'sub': 2', '4, 'a first product stream comprising C-Colefins; and'}a second product ...

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Номер записи: 29
25-02-2021 дата публикации

PROCESS AND PLANT FOR PRODUCING METHANOL FROM SYNTHESIS GASES HAVING A HIGH PROPORTION OF CARBON DIOXIDE

Номер: US20210053898A1
Автор: Castillo-Welter Frank, GRONEMANN Veronika, Haag Stephane, Schuhmann Timm, Williams Bryce
Принадлежит:

The invention relates to a process for producing methanol and to a plant for producing methanol. A first fresh gas suitable for production of methanol and having a high carbon dioxide content is pre-compressed by a first compressor stage to obtain a second fresh gas. The second fresh gas is merged with a recycle gas stream and further compressed to synthesis pressure in a second compressor stage. Catalytic conversion of the thus obtained synthesis gas stream in a plurality of serially arranged reactor stages with intermediate condensation and separation of the crude methanol reduces the recycle gas amount in the synthesis circuit to such an extent that recycle gas may be directly recycled to the second fresh gas stream, thus ensuring that no recycle gas compressor stage is required and that the total compressor power may be reduced. 1. A process for producing methanol , comprising:a) providing an input gas comprising carbon oxides and hydrogen, wherein the proportion of carbon dioxide in the input gas, based on the total amount of the carbon oxides, is at least 80% by volume;b) introducing the input gas as a first fresh gas stream into a first compressor stage for precompression of the first fresh gas stream to obtain a second fresh gas stream;c) introducing a recycle gas stream and the second fresh gas stream into a second compressor stage for compression of the recycle gas stream and the second fresh gas stream to synthesis pressure to obtain a synthesis gas stream;d) catalytically converting the synthesis gas of the synthesis gas stream in a plurality of serially arranged reactor stages at synthesis pressure to obtain a product stream comprising methanol and unreacted synthesis gas per reactor stage;e) cooling the product stream obtained per reactor stage for condensation and separation of methanol from unreacted synthesis gas and introducing unreacted synthesis gas into a respective subsequent stage of the serially arranged reactor stages;f) withdrawing ...

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Номер записи: 30
13-02-2020 дата публикации

PROCESS FOR THE MULTI-REACTOR SYNTHESIS OF ZEOLITE CRYSTALS HAVING A CONTROLLED PARTICLE SIZE

Номер: US20200048102A1
Автор: LUTZ CÉCILE, NICOLAS Serge
Принадлежит: Arkema France

The present invention relates to a process for preparing zeolite crystals having a multimodal particle size distribution, and the sizes of which are between 0.02 μm and 20 μm, said process comprising feeding at least two reactors each with a synthesis gel capable of forming zeolite crystals, carrying out a crystallization reaction, in parallel, in each of the at least two reactors, and mixing the reaction media of the at least two reactors, after the start of at least one of the crystallization reactions. 1. Process for preparing zeolite crystals having a multimodal particle size distribution , and the sizes of which are between 0.02 μm and 20 μm , said process comprising at least the following steps:a) preparing a synthesis gel by mixing at least one source of silica, at least one source of alumina and optionally, at least one aqueous alkali or alkaline-earth metal hydroxide solution,b) feeding at least two reactors each with a synthesis gel capable of forming zeolite crystals,c) carrying out a crystallization reaction, in parallel, in each of the at least two reactors,d) mixing the reaction media of the at least two reactors, ande) filtering the mixture of the reaction media obtained in step d), in order to separate the crystals produced from the mother liquors.2. Process according to claim 1 , wherein the at least two reactors are each fed by a synthesis gel of zeolite crystals claim 1 , it being possible for the synthesis gels to be identical or different.3. Process according to claim 1 , wherein one or more seeding agents are introduced into the synthesis gel(s) upstream of or inside at least one of the synthesis reactors or in the at least two synthesis reactors.4. Process according to claim 1 , wherein the seeding agent is chosen from nucleating gels claim 1 , zeolite crystals claim 1 , mineral particles claim 1 , and mixtures thereof.5. Process according to claim 1 , wherein the reactors used are stirred reactors for syntheses in batch mode and tubular ...

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Номер записи: 31
04-03-2021 дата публикации

Process for Preparing Fluorobenzene Derivatives and Benzoic Acid Hypofluorite Derivatives

Номер: US20210061737A1
Автор: DU Hongjun, Wu Wenting, Zhou Changyue
Принадлежит: Fujian Yongjing Technology Co., Ltd

The invention relates to a use of a fluorination gas, and the elemental fluorine (F) is preferably present in a high concentration, for example, in a concentration of elemental fluorine (F), especially of equal to much higher than 15% or even 20% by volume, and to a process for the manufacture of a fluorinated benzene derivative starting from benzoic acid derivative by direct fluorination employing a fluorination gas, wherein the elemental fluorine (F) is preferably present in a high concentration, and subsequent decarboxylation of the benzoic acid hypofluorite derivative obtained by direct fluorination. The process of the invention is also directed to the manufacture of a benzoic acid hypofluorite derivative by direct fluorination of benzoic acid derivative. Especially the invention is of interest in the preparation of fluorinated benzene derivative, final products and as well intermediates, for usage in agro-, pharma-, electronics-, catalyst, solvent and other functional chemical applications. 1. A process for the manufacture of a fluorinated benzene derivative , preferably monofluorobenzene derivative , wherein the process comprises the steps of:a) provision of a liquid medium comprising benzoic acid derivative as starting compound;{'sub': '2', 'b) provision of a fluorination gas comprising or consisting of elemental fluorine (F), preferably wherein the fluorine is present in the fluorination gas in a high concentration of at least substantially more than, in particular very much more than 15% by volume (vol.-%), preferably equal to or more than 20% by volume (vol.-%);'}{'sub': '2', 'c) provision of a first reactor or reactor system, resistant to elemental fluorine (F) and hydrogen fluoride (HF);'}{'sub': '2', 'd) in a step of direct fluorination, passing the fluorination gas of b), in a reactor or reactor system of c), through the liquid medium of a) comprising the benzoic acid derivative as starting compound, and thereby reacting the benzoic acid derivative ...

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Номер записи: 32
20-02-2020 дата публикации

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Номер: US20200055796A1
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. 1. A system , comprising:{'sub': 2', '4', '2', '4', '3', '6', '2', '2', '4, 'an ethylene-to-liquids (ETL) reactor that (i) receives an olefin feed stream at a first temperature, said olefin feed stream comprising (1) ethylene (CH) at a concentration of at least about 0.5 mole percent (mol %), (2) CHand propylene (CH) at a combined concentration of at most about 10 mol %, and (3) carbon monoxide (CO) or carbon dioxide (CO), and (ii) as part of an ETL process, facilitates conversion of CHto higher hydrocarbon products with the aid of an ETL catalyst to yield a product stream comprising said higher hydrocarbon products that is at a second temperature which is higher than said first temperature, wherein said ETL process liberates heat, wherein said higher hydrocarbon products comprise an olefin compound and an aromatic compound; and'}a separations module in fluid communication with said ETL reactor that recovers from said product stream a liquid stream comprising said higher hydrocarbon products, wherein said higher hydrocarbon products include (i) at least 5 compounds having 5 different carbon numbers, said 5 different carbon numbers selected from 4 through 20, wherein each of said at least 5 compounds is at a concentration of at least 5 weight percent (wt %) of said liquid stream, and (ii) a paraffin compound, an isoparaffin compound, and a naphthene compound,wherein at least about 80% of said heat liberated in said ETL process provides a difference between said first temperature and said second temperature of between about 50° C. and about 150° C.2. The system ...

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Номер записи: 33
11-03-2021 дата публикации

METHOD FOR PRODUCING TETRAFLUOROETHYLENE AND/OR HEXAFLUOROPROPYLENE

Номер: US20210070679A1
Автор: Hirai Mai, Nakaya Hideki, Noguchi Atsushi, OHTA Toshihiko, Yasuhara Takashi
Принадлежит: DAIKIN INDUSTRIES, LTD.

A process for producing one or both of tetrafluoroethylene and hexafluoropropylene, which includes pyrolyzing a low molecular weight fluorine compound by continuous reaction in a microreactor. 1. A process for producing at least one of tetrafluoroethylene and hexafluoropropylene , comprising:pyrolyzing a low molecular weight fluorine compound by continuous reaction in a microreactor.2. The process according to claim 1 , wherein the low molecular weight fluorine compound has a carbon chain having 4 to 28 carbon atoms.3. The process according to claim 1 , wherein the low molecular weight fluorine compound has a carbon chain having 4 to 18 carbon atoms.4. The process according to claim 1 , wherein the low molecular weight fluorine compound is a perfluoroalkene.5. The process according to claim 1 , wherein the pyrolysis is performed in the temperature range of 620° C. to 720° C.6. The process according to claim 1 , wherein a diameter of the microreactor is 1 mm to 20 mm.7. The process according to claim 1 , wherein the pyrolysis is performed in the condition of mixing the low molecular weight fluorine compound and an inert gas. This is a continuation application under 37 C.F.R. § 1.53(b) of PCT/JP2019/019722 filed May 17, 2019, which claims priority from Japanese Patent Application No. 2018-096506 filed May 18, 2018, incorporated herein by reference in its entirety.The present disclosure relates to a process for producing tetrafluoroethylene and/or hexafluoropropylene.The pyrolysis of a perfluoroalkane is known as a method for producing tetrafluoroethylene and hexafluoropropylene (Patent Literature 1). In Patent Literature 1, a perfluoroalkane was added to a cylindrical container, heated and pyrolyzed to obtain tetrafluoroethylene and hexafluoropropylene.Patent Literature 1: Japanese Patent Laid-Open No. 2016-13994The method of Patent Literature 1 has a problem that the conversion ratio and the selection ratio from a perfluoroalkane to tetrafluoroethylene and ...

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Номер записи: 34
11-03-2021 дата публикации

Process of Removing Heat

Номер: US20210070681A1
Автор: Dolan John, GREAGER Ivan Phillip, HARRIS Roger Allen, LeViness Stephen Claude, PARKER Dennis, RAMLAL Jasmeer Jaichland, STEYNBERG Andre Peter
Принадлежит:

The present invention provides an improved process for removing heat from an exothermic reaction. In particular, the present invention provides a process wherein heat can be removed from multiple reaction trains using a common coolant system. 120-. (canceled)21. A method of starting up an exothermic reaction comprising:(a) providing at least two separate reaction trains each comprising at least one reactor;(b) providing a common coolant circulation system which comprises a single common reservoir comprising a coolant which is fed into each reaction train;(c) starting circulation of the coolant to each reaction train;(d) increasing the pressure the reactors to a desired reaction pressure;(e) feeding a reactant feedstream into each reaction train;(f) increasing the temperature of the single common reservoir while adjusting the GHSV of the reactant feedstreams through each reaction train to obtain the desired extent of exothermic reaction.2226-. (canceled)27. A method of starting up an exothermic reaction in a start-up reactor comprised in a reaction train , said method comprisinga) providing multiple reaction trains each comprising at least one reactor;b) providing a common coolant circulation system which comprises a single common reservoir comprising a first coolant which is fed into each reaction train except the reaction train comprising the start-up reactor in which the exothermic reaction is to be started up;c) providing a second coolant circulation system associated with a second coolant reservoir comprising a second coolant which is fed into the reaction train comprising the start-up reactor;d) increasing the pressure in the start-up reactor to a desired reaction pressure;e) feeding a reactant feedstream into the reaction train comprising the start-up reactor;f) running the process until the operating conditions of the start-up reactor are such that the coolant exiting the start-up reactor may be reintroduced to the common coolant circulation system; andg) ...

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Номер записи: 35
15-03-2018 дата публикации

PROCESS OF REMOVING HEAT

Номер: US20180072643A1
Автор: Dolan John, GREAGER Ivan Phillip, HARRIS Roger Allen, LeVINESS Steven Claude, PARKER Dennis, RAMLAL Jasmeer Jaichland, STEYNBERG Andre Peter
Принадлежит:

The present invention provides an improved process for removing heat from an exothermic reaction. In particular, the present invention provides a process wherein heat can be removed from multiple reaction trains using a common coolant system. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. (canceled)14. (canceled)15. (canceled)16. (canceled)17. (canceled)18. (canceled)19. (canceled)20. (canceled)21. (canceled)22. A method of isolating a reaction train from an exothermic reaction process circuit which comprises multiple reaction trains to which a first coolant is fed from a common first coolant reservoir and wherein each reaction train comprises a reactor to which a reactant substream is fed , comprising:performing the exothermic reaction in the reactor to produce reaction products and first coolant to which heat has been transferred;providing a second coolant circulation system associated with a second coolant reservoir;redirecting the first coolant to which heat has been transferred from the reaction train to be isolated to the second coolant reservoir; and thenstopping the feed of the first coolant to the reaction train to be isolated while simultaneously initiating the feed of the second coolant from the second coolant reservoir to the reaction train to be isolated.23. The method according to claim 22 , wherein the first coolant and the second coolant are the same.24. The method according to claim 22 , wherein the first coolant and the second coolant are different.25. A method of reintroducing a reaction train which has been isolated from an exothermic reaction process circuit which comprises multiple reaction trains to which a first coolant is fed from a common coolant reservoir claim 22 , wherein each reaction train comprises a reactor to which a reactant substream is fed and wherein:an exothermic reaction is performed in the reactor of each ...

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Номер записи: 36
24-03-2022 дата публикации

Continuous processes for the selective conversion of aldohexose-yielding carbohydrate to ethylene glycol using low concentrations of retro-aldol catalyst

Номер: US20220089515A1
Автор: Brooke ALBIN, David James Schreck, Donald Bunning, Louis A. Kapicak, Mark Nunley, Michael Bradford
Принадлежит: TEn Process Technology Inc, TEn Stone & Webster Process Technology Inc

Retro-aldol processes are disclosed that use very low concentrations of retro-aldol catalyst in combination with hydrogenation catalyst of certain activities, sizes and spatial dispersions to obtain the high selectivities to ethylene glycol.

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Номер записи: 37
07-03-2019 дата публикации

PROCESS FOR THE PREPARATION OF AN ALKANESULFONIC ACID

Номер: US20190071394A1
Автор: CHEUNG Chiu Kee, Fonfe Benjamin, HARTWIG Ali
Принадлежит: EVONIK DEGUSSA GmbH

The present invention relates to a process for the preparation of an alkanesulfonic acid by oxidation of a sulfur containing starting compound with an oxygen containing fluid, wherein the sulfur containing starting compound is provided in a reaction system, comprising a reaction vessel () with an expansion vessel () on its top, wherein the reaction vessel and the expansion vessel are connected to allow a flow of a fluid stream from the reaction vessel into the expansion vessel. 1. A process for preparing an alkanesulfonic acid by oxidation of a starting compound comprising sulfur with a fluid comprising oxygen , the method comprising:providing the starting compound in a reaction system,wherein the reaction system comprises a reaction vessel and an expansion vessel on top of the reaction vessel, wherein the reaction vessel and the expansion vessel are connected to allow a flow of a fluid stream from the reaction vessel into the expansion vessel.2. The process according to claim 1 , wherein the reaction vessel is completely flooded with a liquid phase.3. The process according to claim 2 , wherein a liquid volume withdrawn from the reaction system equals a volume of the liquid phase entering the reaction system claim 2 , when the process is operated in continuous or semi-continuous mode.4. The process according to claim 1 , wherein a reaction pressure within the reaction system is regulated by means of a pressure controlling valve.5. The process according to claim 1 , wherein a volume of the expansion vessel is smaller than a volume of the reaction vessel.6. The process according to claim 1 , wherein a concentration of the starting compound in a gas phase is monitored by means of an online analysis device claim 1 , an offline analysis device claim 1 , or both.7. The process according to claim 6 , wherein the concentration of the starting compound in the gas phase is monitored online by means of an Fourier transform infrared spectrometer claim 6 , offline by means of a ...

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Номер записи: 38
15-03-2018 дата публикации

Treatment of degraded oxime metal extractants in process organic solutions

Номер: US20180073099A1
Автор: Erkki Paatero, James Kabugo
Принадлежит: Outotec Finland Oy

The invention relates to a method for regenerating the extractive potential of an organic hydroxyoxime-based extraction solution used in the recovery of metals by liquid-liquid extraction. The method is two-stage, in which a solid hydroxylamine is used in the reaction stage, and the removal of the undesirable compounds generated in the reaction occurs in the second stage by adsorption purification. The method of the invention is suitable for treatment of degraded oxime metal extractants in various process organic solutions both in aldehyde and ketoxime extractant solutions. The method can also be used to treat a mixture of degraded oxime extractants.

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Номер записи: 39
24-03-2022 дата публикации

METHOD FOR CONTINUOUSLY PRODUCING AROMATIC POLYETHER

Номер: US20220089815A1
Автор: KURIU Toshiyuki, SUZUKI Tasutaka
Принадлежит: KUREHA CORPORATION

A method for continuously producing an aromatic polyether according to the present invention includes simultaneously implementing: a supply step of supplying a polymerization solvent, an alkali metal compound, and a raw material; a polymerizing step; and a movement step. The alkali metal compound is supplied as an aqueous mixture. According to the present invention, clogging of piping in the continuous production apparatus can be suppressed, and the aromatic polyether can be stably obtained. 2. (canceled)3. The continuous production method according to claim 1 , wherein the raw material is in the form of a solution in which the raw material is dissolved in the polymerization solvent.4. The continuous production method according to claim 1 , wherein a pH of the reaction mixture in at least one or more of the reaction vessels is from 9 to 12.5.5. The continuous production method according to claim 1 , wherein in at least one of the reaction vessels claim 1 , the reaction mixture comprises the aromatic polyether having a weight average molecular weight from 2000 to 50000 claim 1 , and the pH of the reaction mixture in at least one of the at least one reaction vessel is from 9 to 12.5.6. The continuous production method according to claim 1 , wherein the raw material comprises an aromatic dihalogen compound and an aromatic dihydroxy compound.7. The continuous production method according to claim 1 , wherein the alkali metal compound comprises an alkali metal carbonate.8. The continuous production method according to claim 1 , wherein the aromatic polyether is a polyaryletherketone.9. The continuous production method according to claim 8 , wherein the polyaryletherketone is polyether ether ketone.10. The continuous production method according to claim 1 , wherein the aromatic polyether is an aromatic polysulfone.11. The continuous production method according to claim 10 , wherein the aromatic polysulfone is a polysulfone claim 10 , polyphenylsulfone claim 10 , or ...

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Номер записи: 40
05-03-2020 дата публикации

System and Method for Monitoring and Controlling a Polymerization System

Номер: US20200070118A1
Автор: Hert Daniel G., NETEMEYER Eric J., Schwerdtfeger Eric D.
Принадлежит:

The present disclosure relates generally to a system having a reactor system with a polymerization reactor and a feed system fluidly coupled to a feed inlet of the reactor. The feed system supplies components to the reactor via the feed inlet, and the reactor has a flow path that continuously conveys the components through the reactor and subjects the components to polymerization conditions to produce a polymer. The system also has an analysis system coupled to the reactor for online monitoring of a particle size of the polymer. Further, the system includes a control system, coupled to the analysis and feed systems, that receives a signal from the analysis system indicative of the monitored particle size of the polymer and adjusts an operating parameter of the feed system to control a flow rate of at least one of the components to the reactor based at least on the signal. 1. A polymerization system , comprising:a reactor system comprising a polymerization reactor and a feed system fluidly coupled to a feed inlet of the polymerization reactor, wherein the feed system is configured to supply polymerization components to the polymerization reactor via the feed inlet, and the polymerization reactor comprises a flow path configured to continuously convey the polymerization components through an interior of the polymerization reactor and configured to subject the polymerization components to polymerization conditions to produce a polymer slurry comprising polymer particles;an analysis system coupled to the polymerization reactor along the flow path, wherein the analysis system is configured to monitor a particle size of the polymer; anda control system coupled to the analysis system and the feed system, wherein the control system is configured to receive a signal from the analysis system indicative of the monitored particle size of the polymer particles, and is configured to adjust an operating parameter of the feed system to control a flow rate of at least one of the ...

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Номер записи: 41
05-03-2020 дата публикации

ETHYLENE-TO-LIQUIDS SYSTEMS AND METHODS

Номер: US20200071242A1
Автор: Bergstrom Peter, Cizeron Joel, Czerpak Peter, Faz Carlos, Iyer Rahul, 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. 1111.-. (canceled)112. A method , comprising:(a) directing an olefin-containing stream comprising an olefin into an ethylene-to-liquids (ETL) reactor comprising an ETL catalyst that facilitates conversion of at least a portion of said olefin to higher hydrocarbon compounds to yield an ETL product stream comprising said higher hydrocarbon compounds;{'sub': 4+', '3, '(b) directing at least a portion of said ETL product stream into a de-propanizer that separates said higher hydrocarbon compounds into a bottom stream comprising hydrocarbon compounds with four or more carbon atoms (C compounds) and an overhead stream comprising hydrocarbon compounds with three carbon atoms (Ccompounds); and'}{'sub': '3', '(c) directing at least a portion of said Ccompounds into said ETL reactor.'}113. The method of wherein said olefin comprises ethylene claim 112 , propylene claim 112 , or a combination thereof.114. The method of claim 112 , further comprising claim 112 , prior to (a) claim 112 , directing a hydrocarbon feedstream comprising feedstream hydrocarbons into a cracking reactor comprising a cracking catalyst that facilitates a cracking of said feedstream hydrocarbons to produce a cracked stream comprising cracked hydrocarbons claim 112 , wherein said cracked hydrocarbons have a lower molecular weight than said feedstream hydrocarbons claim 112 , and using at least a subset of said cracked hydrocarbons to generate said olefin-containing stream.115. The method of claim 114 , further comprising directing said cracked stream into a separations unit that separates said ...

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Номер записи: 42
18-03-2021 дата публикации

Slurry Loop Reactor Bad Catalyst Range Control

Номер: US20210077972A1
Автор: Mcgee Maxwell T., Picou Douglas J., Poindexter Ariana L., Quant Asha C., Trapp Keith W.
Принадлежит:

A process for maintaining an optimum polymerization process in a continuous loop polymerization reactor by driving a catalyst feed range set-point around a bad catalyst set-point range using a bad catalyst feed rate program to vary the catalyst feed rate for differing periods of time between previously determined good catalyst feed rates. 1. A process for maintaining an optimum polymerization conditions in a continuous loop polymerization reactor by driving a catalyst feed range set-point around a bad catalyst set-point range , comprising:if there is a non-optimum polymerization condition requiring a change in a catalyst feed rate, calculating a desired catalyst feed rate to return the process to optimum conditions;sending the desired catalyst feed rate to a bad catalyst program for determining whether the desired catalyst feed rate falls within a bad catalyst feed rate set-point range;if the desired catalyst feed rate is determined to fall within the bad catalyst feed rate set-point range, turning over control of the catalyst feed rate to the bad catalyst program,wherein the bad catalyst program controls and incrementally changes the catalyst feed rate set-point delivered by a semi-continuous shot feeder between previously established first and second good catalyst feed rate set-points, above and below the bad catalyst feed rate set-point range, so that an average catalyst feed rate is equivalent to the desired catalyst feed rate set-point within the bad catalyst feed rate set-point range.2. The process of claim 1 , wherein the bad catalyst program determines a first period of time required for the catalyst feed rate to remain at the first good catalyst feed rate set-point claim 1 , and a second period of time required for the catalyst feed rate to remain at the second good catalyst feed rate set-point claim 1 , to establish a time-weighted average catalyst feed rate which is equivalent to the desired catalyst feed rate set-point within the bad catalyst feed rate ...

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Номер записи: 43
12-06-2014 дата публикации

Apparatus and process for the controlled reduction of organic material via microwave radiation

Номер: US20140161680A1
Автор: Stephen P. Simms, Steven L. Kantor
Принадлежит: Individual

A controllable, continuous-feed system and process for the reduction or depolymerization of organic materials using microwave energy in a reducing, substantially oxygen-reduced atmosphere. The microwave energy is generated by a plurality of magnetrons in a microwave tunnel. Gaseous products may be extracted from the microwave tunnel for recycling and/or analysis. A collector such as a liquid trap may be used to separately collect floating and sinking constituents of the solid products while preventing the escape of the reducing atmosphere from the system.

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Номер записи: 44
23-03-2017 дата публикации

Polyethylene production with multiple polymerization reactors

Номер: US20170081436A1
Автор: Catherine M. Gill, Elizabeth Ann 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 discharging a transfer slurry from a first polymerization reactor through a transfer line to a second polymerization reactor, the transfer slurry including at least diluent and a first polyethylene. A product slurry is discharged from the second polymerization reactor, the product slurry including at least diluent, the first polyethylene, and a second polyethylene. The velocity, pressure drop, or pressure loss due to friction in the transfer line is determined, and a process variable adjusted in response to the velocity, pressure drop, or pressure loss not satisfying a specified value.

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Номер записи: 45
26-03-2015 дата публикации

METHOD FOR PRODUCING ACROLEIN AND/OR ACRYLIC ACID FROM GLYCEROL

Номер: US20150087861A1
Автор: Devaux Jean-Francois, Fauconet Michel, Tlili Nabil
Принадлежит:

The invention relates to the production of acrolein and/or acrylic acid from glycerol, and more particularly to a method for continuous production of a stream comprising acrolein by dehydration of glycerol, comprising cycles of reaction and regeneration of a dehydration catalyst. 1. A method for continuous production of a stream comprising acrolein , comprising the steps of:a) reacting a gaseous reaction stream comprising glycerol, by contacting said gaseous reaction stream with a solid acid catalyst in a reactor zone maintained at a temperature in the range from 250° C. to 350° C. to obtain a converted stream comprising acrolein, (i) step (b) is carried out at a regeneration temperature similar to the reaction temperature of step (a), and', '(ii) a hot spot of the catalyst during step (b) does not exceed 100° C. above the temperature of the reactor zone containing the catalyst in regeneration mode, and', '(iii) step (a) and step (b) are applied simultaneously, each on at least one reactor zone in the form of cycles in reaction mode and in regeneration mode offset from one zone to another., 'b) regenerating said solid catalyst with a gaseous regeneration stream comprising oxygen, wherein2. The method of wherein step (a) and step (b) are carried out on two or more catalyst zones placed in at least two reactors in parallel claim 1 , each reactor being supplied separately.3. The method of wherein step (a) and step (b) are carried out in one same reactor comprising at least 2 catalyst zones claim 1 , each zone being supplied separately.4. The method of wherein the number of catalyst zones operating in reaction mode is equal to the number of zones operating in regeneration mode.5. The method of wherein the number of catalyst zones operating in reaction mode is greater than the number of zones operating in regeneration mode.6. The method of wherein the regeneration stream contains water.7. The method of wherein an increasing temperature gradient is applied to the reactor ...

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Номер записи: 46
12-03-2020 дата публикации

A METHOD FOR THE PRODUCTION OF HIGH PURITY BUTADIENE AND N-BUTENE FROM N-BUTANE USING AN OXIDATIVE DEHYDROGENATION PROCESS IN A CONTINUOUS-FLOW MULTI-LAYER-CATALYST FIXED-BED REACTOR

Номер: US20200079710A1
Автор: Bunama Ramsey, Choi YongMan, JAMALEDDINE Tarek Jamal
Принадлежит:

Systems and methods for the production of n-butene isomers and/or 1,3-butadiene are disclosed. The systems and method involve an oxidative dehydrogenation (ODH) process for the production of n-butene isomers and 1,3-butadiene light olefins using an adjustable, multi-purpose, and multi-layer-catalyst bed for a reactor. 1. A method of producing n-butene (CHCHCH═CH) and/or 1 ,3-butadiene (HC═CH—CH═CH) , the method comprising:{'sub': 4', '4', '10, 'flowing a feed stream comprising Chydrocarbons, including n-butane (CH), to a reactor, the reactor including a catalyst bed that comprises three separate catalytic layers arranged in series with respect to the flow of the feed stream, wherein a first inert layer of material is disposed between a first catalytic layer of the three separate catalytic layers and a second catalytic layer of the three separate catalytic layers, wherein a second inert layer of material is disposed between the second catalytic layer and a third catalytic layer of the three separate catalytic layers,'}contacting the n-butane with the first catalytic layer under reaction conditions sufficient to convert n-butane to n-butene and 1,3-butadiene, wherein the first catalytic layer is adapted to catalyze conversion of n-butane to n-butene and 1,3-butadiene; andflowing n-butene and/or 1,3-butadiene from the reactor.2. The method of claim 1 , wherein the feed stream comprises primarily n-butane.3. The method of claim 1 , wherein the feed stream comprises 85 to 99 wt. % n-butane claim 1 , 1 to 10 wt. % of n-butene claim 1 , and 0 to 5 wt. % of residual Ccompounds.4. The method of claim 1 , wherein each catalytic layer comprises different catalytic materials from the other catalytic layers.5. The method of claim 1 , further comprising:contacting a first portion of the n-butene with the second catalytic layer under reaction conditions sufficient to convert the first portion of the n-butene to 1,3-butadiene, wherein the second catalytic layer is adapted to ...

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Номер записи: 47
12-03-2020 дата публикации

PROCESS FOR ACID-CATALYZED DECOMPOSITION OF ARYL a- HYDROPEROXIDE WITH CONTINUOUS FLOW TUBULAR REACTOR

Номер: US20200079714A1
Автор: "SUN Fuan", CHEN Qun, DAI Xuan, HE Mingyang, SUN ZHONGHUA, ZHOU Weiyou
Принадлежит: CHANGZHOU UNIVERSITY

The present disclosure relates to a process for acid-catalyzed decomposition of aryl α-hydroperoxide with a continuous flow tubular reactor. The process is a novel process performed in a tubular reactor, taking the aryl α-hydroperoxide such as cumene hydroperoxide (CHP) as a raw material and taking acids as a catalyst, performing acid-catalyzed decomposition of the aryl α-hydroperoxide solution in a short reaction time ranging from tens of seconds to several minutes, thereby obtaining the phenols; wherein an inert component may be filled in the reactor, so that the effects of heat transmission and mass transfer can be enhanced. The aryl α-hydroperoxide and acid are respectively introduced by a metering pump into a mixing module to be mixed, and then enter the tubular reactor to be reacted so as to produce the products such as phenols. 3. The process for acid-catalyzed decomposition of aryl α-hydroperoxide with a continuous flow tubular reactor according to claim 1 , wherein the aryl α-hydroperoxide is cumyl hydroperoxide (CHP).4. The process for acid-catalyzed decomposition of aryl α-hydroperoxide with a continuous flow tubular reactor according to claim 1 , wherein the process further comprises the following step (2):(2) the concentration of each substance in the reaction products is analyzed by a liquid chromatography external standard method, and the aryl α-hydroperoxide is titrated by an iodometric method.5. The process for acid-catalyzed decomposition of aryl α-hydroperoxide with a continuous flow tubular reactor according to claim 3 , wherein the CHP in step (1) is a concentrated oxidation liquid of cumene claim 3 , the solvent is one of acetone and cumene or a mixture thereof; or the oxidation liquid of cumene is used as a source of the CHP.6. The process for acid-catalyzed decomposition of aryl α-hydroperoxide with a continuous flow tubular reactor according to claim 1 , wherein the acid in step (1) is one or more selected from a group consisting of sulfuric ...

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Номер записи: 48
12-03-2020 дата публикации

PROCESS FOR PRODUCING (METH)ACRYLIC ESTERS

Номер: US20200079722A1
Автор: DUBUT Fanny, ESCH Marc, GRAIRE Coralie, RIFLADE Benoit
Принадлежит:

This invention relates to a process for the continuous production of a (meth)acrylic ester by transesterification reaction between a C1-C4 light alkyl (meth)acrylate, with a heavy alcohol in the presence of a catalyst, characterised in that the flows feeding the reactor are introduced through a static mixer placed on a recirculation loop of the reactor. The use of a static mixer improves the selectivity of the reaction and consequently the overall productivity of (meth)acrylic ester synthesis process. 1. A process for continuous production of a (meth)acrylic ester by transesterification reaction between a light alkyl (meth)acrylate selected from the group consisting of methyl (meth)acrylate and ethyl (meth)acrylate , with a heavy alcohol in the presence of a catalyst , wherein flows feeding the reactor are introduced through a static mixer which is a pipe element with propellers or baffles or other obstacle to increase turbulence , placed on a recirculation loop of reagents , catalyst and recycled flows upstream of the reactor.2. The process according to claim 1 , wherein the static mixer is placed upstream of the reactor reboiler.3. The process according to claim 1 , wherein the static mixer is placed downstream of the reactor reboiler.4. The process according to wherein the heavy alcohol is a linear or branched claim 1 , primary or secondary alcohol comprising between 4 and 12 carbon atoms claim 1 , optionally comprising at least one nitrogen atom.5. The process according to wherein the heavy alcohol is an amino alcohol of formula (II):{'br': None, 'sub': 2', '3, 'HO-A-N(R′)(R′) \u2003\u2003(II)'}wherein{'sub': 1', '5, 'A is an alkylene radical, linear or branched, in C-C'}{'sub': 2', '3', '1', '4, 'R′and R′, which are identical or different from one another, each representing a C-Calkyl radical.'}6. The process according to wherein the heavy alcohol is N claim 1 ,N-dimethylaminoethanol (DMAE) claim 1 , N claim 1 ,N-diethylaminoethanol claim 1 , or N claim 1 ,N- ...

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Номер записи: 49
21-03-2019 дата публикации

System and Method for Monitoring and Controlling a Polymerization System

Номер: US20190083950A1
Автор: Hert Daniel G., NETEMEYER Eric J., Schwerdtfeger Eric D.
Принадлежит:

The present disclosure relates generally to a system having a reactor system with a polymerization reactor and a feed system fluidly coupled to a feed inlet of the reactor. The feed system supplies components to the reactor via the feed inlet, and the reactor has a flow path that continuously conveys the components through the reactor and subjects the components to polymerization conditions to produce a polymer. The system also has an analysis system coupled to the reactor for online monitoring of a particle size of the polymer. Further, the system includes a control system, coupled to the analysis and feed systems, that receives a signal from the analysis system indicative of the monitored particle size of the polymer and adjusts an operating parameter of the feed system to control a flow rate of at least one of the components to the reactor based at least on the signal. 1. A polymerization system , comprising:a reactor system comprising a polymerization reactor and a feed system fluidly coupled to a feed inlet of the polymerization reactor, wherein the polymerization reactor comprises segments of reactor piping connected by elbows or bends, wherein the feed system is configured to supply polymerization components to the polymerization reactor via the feed inlet, and wherein the reactor system comprises a flow path configured to continuously convey the polymerization components through the segments of reactor piping from the feed inlet through an outlet line fluidly connected with the polymerization reactor, and wherein the polymerization components are subjected to polymerization conditions within the polymerization reactor to produce a polymer slurry comprising polymer particles;an analysis system coupled to the polymerization reactor along the flow path, wherein the analysis system is configured to monitor a particle size of the polymer particles; anda control system coupled to the analysis system and the feed system, wherein the control system is configured to ...

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Номер записи: 50
29-03-2018 дата публикации

CONTINUOUS PROCESSES FOR THE HIGHLY SELECTIVE CONVERSION OF SUGARS TO PROPYLENE GLYCOL OR MIXTURES OF PROPYLENE GLYCOL AND ETHYLENE GLYCOL

Номер: US20180086681A1
Автор: Albin Brooke, Bradford Marion McKinley, Bunning Donald, Chrisman Ray, Clinton Nye, Schreck David James
Принадлежит:

Continuous processes for making propylene glycol from ketose-yielding carbohydrates are disclosed which enhance the selectivity to propylene glycol. 2. The process of wherein the feed comprises ketose-yielding and aldose-yielding carbohydrate and a mixture of propylene glycol and ethylene glycol is contained in the product solution.3. The process of wherein the feed comprises sucrose.4. The process of wherein the product solution contains a mass ratio of 1 claim 1 ,2-butanediol to total propylene glycol and ethylene glycol of less than about 1:10.5. The process of wherein the aqueous solution is maintained at a temperature of greater than about 170° C. and less than 230° C. for less than about 15 seconds prior to being passed into the aqueous-hydrogenation medium.6. The process of wherein the heating of the carbohydrate feed from below 170° C. to above 230° C. is at least in part by direct heat exchange by admixing the carbohydrate feed with a warmer fluid.7. The process of wherein the warmer fluid comprises the aqueous-hydrogenation medium.8. The process of wherein the admixing of the carbohydrate feed and warmer fluid involves high shear mixing.9. The process of wherein the admixing of the carbohydrate feed and warmer fluid involves rapid diffusional mixing.10. The process of wherein the heating of the carbohydrate feed from below 170° C. to above 230° C. is at least in part by indirect heat exchange.14. The process of wherein the heating of the carbohydrate feed from below 170° C. to above 230° C. occurs whereupon the carbohydrate is contacted with an aqueous claim 1 , retro-aldol solution containing retro-aldol catalyst in the substantial absence of hydrogenation catalyst.15. The process of wherein the carbohydrate-containing feed contains between about 120 and 800 grams of carbohydrate per liter of aqueous-hydrogenation medium.16. The process of wherein the carbohydrate-containing feed contains aldose and the rate of heating of the carbohydrate feed from below ...

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Номер записи: 51
02-04-2015 дата публикации

PROCESS FOR THE PRODUCTION OF HEXAMETHLENEDIAMINE

Номер: US20150093301A1
Автор: Alini Stefano, Corona Alberto, Crippa Tommaso, Guida Luciano
Принадлежит:

It is described a process for the production of hexamethylenediamine by hydrogenation of adiponitrile, comprising an improved step of regeneration of the catalyst. Also described are an equipment for the production of hexamethylenediamine, and a washing apparatus () for implementing the catalyst regeneration step. 1. An apparatus for the production of hexamethylenediamine , comprising:a vertical tubular reaction vessel having an ejection device positioned inside said vertical tubular reaction vessel for promoting the agitation of the reaction medium;a separation device positioned in a top part of said vertical tubular reaction vessel for enabling the separation of a gas-phase from a liquid-phase in a reaction medium; a pipe connecting said drawing off device to a first tank;', 'a pipe connecting said vertical tubular reaction vessel to a top part of a washing apparatus;', 'a pipe feeding water to a bottom of said washing apparatus;', 'a pipe connecting the top part of said washing apparatus to said first tank;', 'a pipe connecting the bottom of said washing apparatus to a sedimentation tank, the sedimentation tank including a bottom connected to said pipe for feeding a regenerated catalyst;', 'a pipe connecting a bottom of said first tank to a second tank where alkali phase separation occurs;', 'a pipe connected to said second tank extracting hexamethylenediamine-water solution; and pipes connected to said second tank and said sedimentation tank for extracting wastes., 'a drawing off device positioned in the top part of said vertical tubular reaction vessel for enabling the drawing off of the reaction product, said drawing off device including a top part connected through a gas pipe to a gas re-cycling pump for feeding back hydrogen to a bottom of the vertical tubular reaction vessel, said bottom part of the vertical tubular reaction vessel connected to a pipe for feeding adiponitrile, a pipe for feeding regenerated catalyst, a pipe for the feeding aqueous solution ...

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Номер записи: 52
30-03-2017 дата публикации

METHOD FOR PRODUCING ACROLEIN AND/OR ACRYLIC ACID FROM GLYCEROL

Номер: US20170088500A1
Автор: Devaux Jean-Francois, Fauconet Michel, Tlili Nabil
Принадлежит:

The invention relates to the production of acrolein and/or acrylic acid from glycerol, and more particularly to a method for continuous production of a stream comprising acrolein by dehydration of glycerol, comprising cycles of reaction and regeneration of a dehydration catalyst. 2. The installation as claimed in comprising a single device for withdrawing gas mixture.3. The installation as claimed in claim 2 , wherein each of the reactor zones has fluidic connection to a device for withdrawing gas mixture.410204020. The installation as claimed in claim 1 , wherein the reactor R is a multiple-tube reactor comprising tubes () fixed by tube plates () and comprising at least one plate () positioned between the reactor dome and the tube plates (). This application is a divisional application of U.S. Ser. No. 14/395,128, filed Oct. 17, 2014 which is a national stage application under 35 U.S.C. §371 of PCT/FR2013/050730, filed Apr. 3, 2013, which claims benefit to French patent application FR 1253557, filed Apr. 18, 2012, Patented; Patent No. FR 2989684 B1 on Oct. 31, 2014.The work leading to the present invention received financial support from the seventh framework program of the European Community FP7/2007-2013 based on subsidy agreement No. 228867.The present invention relates to the production of acrolein and/or acrylic acid from glycerol, and relates more particularly to a method for continuous production of a stream comprising acrolein by dehydration of glycerol, comprising cycles of reaction and regeneration of the dehydration catalyst.It also relates to a plant for producing this continuous stream of acrolein efficiently in terms of energy consumption and productivity, without high capital costs and in good conditions of safety.TECHNOLOGICAL BACKGROUNDResources of fossil origin, such as petroleum cuts, for the chemical industry will be exhausted some decades from now. That is why, for some years, industrial corporations have oriented their research and development ...

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Номер записи: 53
19-03-2020 дата публикации

PROCESS FOR THE POLYMERIZATION OF OLEFINS

Номер: US20200087421A1
Автор: Alshaiban Ahmad Abdullah, Banat Yahya, Maidan Osamah
Принадлежит:

The present invention relates to a process for the continuous preparation of a polyolefm in a reactor from one or more α-olefm monomers of which at least one is ethylene or propylene, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate, wherein the process comprises—feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate—feeding the one or more α-olefm monomers to the reactor—with-drawing the polyolefm from the reactor—circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are cooled using a heat exchanger, resulting in a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream wherein a stream comprising a thermal run away reducing agent (TRRA-containing stream) is introduced into the expanded section during at least part of the polymerization process, wherein said TRRA-containing stream is brought into contact with at least part of the interior surface of the expanded section. 1. A process for the continuous preparation of a polyolefin in a reactor from one or more α-olefin monomers of which at least one is ethylene or propylene ,wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate', 'feeding the one or more α-olefin monomers to the reactor', 'withdrawing the polyolefin from the reactor', 'circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are cooled using a ...

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Номер записи: 54
12-05-2022 дата публикации

Design and Scheduling of Semi-Batch Chemical-Looping Reactors

Номер: US20220143570A1
Автор: Bollas George M., CHEN CHEN
Принадлежит: University of Connecticut

Systems/methods for continuous operation of fixed bed reactors using gaseous fuels for the purpose of power generation through integration with a combined cycle power plant are provided. The fixed bed reactors are assumed to operate in a semi-batch mode composed of reactor modules that are integrated into module trains that comprise the chemical-looping combustion island of the power plant. The scheduling of each reactor train is cast as an optimization problem that maximizes thermodynamic efficiency subject to constraints imposed to each reactor and the entire island. When the chemical-looping reactors are arranged cyclically, each feeding to or being fed from another reactor, in an operating scheme that mimics simulated moving bed reactors, the thermodynamic efficiency of the reactor island can be improved. Allowing the reversal of module order in the cyclically arranged reactor modules further improves the overall thermodynamic efficiency (to 84.7%), while satisfying constraints imposed for carbon capture, fuel conversion, power plant safety and oxygen carrier stability. 1. A system for chemical-loop reactor-based processing , comprising a plurality of chemical-looping reactors arranged cyclically , each of the plurality of chemical-looping reactors feeding to or being fed from another of the plurality of chemical-looping reactors , in an operating scheme that mimics a simulated moving bed reactor , thereby delivering improved thermodynamic efficiency.2. The system of claim 1 , wherein by allowing reversal of module order in the cyclically arranged chemical-looping reactors claim 1 , overall thermodynamic efficiency is further improved.3. The system of claim 2 , wherein cyclic arrangement of the plurality of chemical-looping reactors achieves a desired level of at least one of carbon capture claim 2 , fuel conversion claim 2 , power plant safety and oxygen carrier stability.4. The system of claim 1 , wherein the plurality of chemical-looping reactors are fixed ...

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Номер записи: 55
05-04-2018 дата публикации

Reactor Systems and Processes Related Thereto

Номер: US20180094083A1
Автор: Paul J. Clymans
Принадлежит: ExxonMobil Chemical Patents Inc

A process for separating components of a reactor off gas is provided. A related reactor system is also provided. The reactor system may include a high pressure tubular reactor and/or an autoclave reactor and may be used for the production polyolefin polymers.

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Номер записи: 56
12-05-2022 дата публикации

Continuous Synthesis Method for 1, 1'-Bicyclic [1.1.1]Pentane-1,3-Diethyl Ketone Compounds

Номер: US20220144744A1
Автор: Che Guanda, HONG Hao, LU Jiangping, Wei Fuliang, Yang Sihang, ZHANG Enxuan
Принадлежит:

Provided is a continuous synthesis method for 1,1′-bicyclic[1.1.1]pentane-1,3-diethyl ketone compounds. The continuous synthesis method comprises: under the irradiation of a light source, continuously conveying raw material A and raw material B to a continuous reaction device for a continuous photochemical reaction to obtain 1,1′-bicyclic[1.1.1]pentane-1,3-diethyl ketone compounds, and controlling the reaction temperature in the continuous reaction device by a temperature control device during the continuous photochemical reaction. A propellane with substituents, as a reaction raw material, is subjected to the above photochemical reaction in the continuous reaction device to reduce the probability of its slow decomposition and deterioration under the irradiation, and greatly improve the conversion rate of the reaction material and product yield. 2. The continuous synthesis method according to claim 1 , wherein R claim 1 , R claim 1 , and Rare each independently selected from hydrogen claim 1 , benzyl claim 1 , methyl claim 1 , phenyl or hydroxy; Rand Rare each independently selected from hydrogen claim 1 , methyl claim 1 , benzyl or phenyl.3. The continuous synthesis method according to claim 1 , wherein before the continuous photochemical reaction claim 1 , the continuous synthesis method further comprises: mixing the raw material A with a solvent to form a mixed solution claim 1 , and then conveying the mixed solution to the continuous reaction device;preferably, the solvent is one or more selected from a group consisting of n-hexane, n-heptane, n-butyl ethere, cyclohexane and cyclopentane.4. The continuous synthesis method of claim 1 , wherein the light source is an LED lamp with a wavelength of 300 to 350 nm.5. The continuous synthesis method according to claim 1 , wherein the reaction temperature of the continuous photochemical reaction is 0 to 30° C. claim 1 , preferably 0 to 5° C.6. The continuous synthesis method according to claim 1 , wherein the reaction ...

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Номер записи: 57
26-06-2014 дата публикации

Process and reactor for dehydration of propanol to propylene

Номер: US20140179972A1
Автор: Brian Ozero, Hassan Taheri, Yogendra Sarin
Принадлежит: PETRON SCIENTECH Inc

A reactor design and configuration and a process for the catalytic dehydration of propanol to propylene where the reactor train is comprised of a multi-stage single reactor vessel or multiple reactor vessels wherein each stage and/or vessel has different length, internal diameter, and volume than the other stages and/or vessels and in addition the stages and/or reactor vessels are connected in series or in parallel arrangement, preferably used with an improved means of introducing the propanol feedstock and a heat carrying inert gas to the improved reactor train.

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Номер записи: 58
26-03-2020 дата публикации

Integrated processing system with continuous acid loop for converting methane to methane-sulfonic acid

Номер: US20200095197A1
Автор: Alan K RICHARDS
Принадлежит: Veolia North America Regeneration Services LLC

Methods and machinery are described for combining methane with sulfur trioxide to make MSA, in a system that sustains optimal concentrations of reactants in the main reactor for high yields, efficiency, and profitability. Rather than simply making MSA and then removing it, this design uses a “continuous loop system” with: (i) a “rich acid” stream containing a high concentration of MSA, mixed with sulfuric acid, which will emerge from the main reactor, and (ii) a “reduced acid” stream containing a low concentration of MSA (still mixed with sulfuric acid), from an extractor unit (such as a distillation unit) which removes some but not all of the MSA from the “rich acid”. Additional subassemblies are described which enable the main reactor to work efficiently, at a sustained high flow-through capacity. This system also can be scaled up or down, for any daily MSA production rate.

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Номер записи: 59
08-04-2021 дата публикации

CO-PRODUCTION OF HIGH PURITY ISOBUTANE AND BUTENE-1 FROM MIXED C4S

Номер: US20210101851A1
Автор: Almering Martinus Johannes, Barias Rosette, Lemoine Romain, Scott Michael Jon
Принадлежит: LUMMUS TECHNOLOGY LLC

Systems and processes disclosed may be used to produce a high purity isobutane stream and a high purity 1-butene stream from mixed C4 streams having disparate starting compositions. 1. A process for the co-production of high purity isobutane and high purity 1-butene streams , the process comprising:providing a first mixed C4 stream and a second mixed C4 stream, each comprising isobutene, isobutane, 1-butene, and 2-butene, and wherein the first mixed C4 stream has a higher concentration of isobutane than the second mixed C4 stream;feeding the first mixed C4 stream and methanol, as a reactant or selectivator, to a first reaction system for converting isobutene contained therein to methyl tert butyl ether or isobutene dimers;feeding the second mixed C4 stream and methanol, as a reactant or selectivator, to a second reaction system for converting isobutene contained therein to methyl tert butyl ether or isobutene dimers;separating an effluent from the first reaction system in a first separation system, including a water wash system, to recover a first lights stream comprising 1-butene, 2-butene, isobutane, a first methanol+water stream, and a first heavy stream comprising the methyl tert butyl ether or the isobutene dimers;separating an effluent from the second reaction system in a second separation system, including a water wash system, to recover a second lights stream comprising 1-butene, 2-butene, and isobutane, a second methanol+water stream, and a second heavy stream comprising the methyl tert butyl ether or the isobutene dimers;feeding the first and second methanol+water streams to a methanol recovery system to separate methanol from the water and returning at least a portion of the methanol to either or both the first and second reaction systems;feeding the second lights stream to a separation system for recovering an isobutane containing stream, a 1-butene stream, and a first heavy C4 stream comprising n-butanes and 2-butene;feeding the isobutane containing ...

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Номер записи: 60
13-04-2017 дата публикации

SELF CLEANING REACTOR SYSTEM

Номер: US20170101354A1
Автор: Brown Stephen, Clavelle Eric, Zoricak Peter
Принадлежит: NOVA CHEMICALS (INTERNATIONAL) S.A.

This invention relates to a self cleaning reactor and to a process for the oligomerization of ethylene that employs a self-cleaning reactor. The reactor includes a mass of inert, particulate cleaning bodies that are entrained by the liquid in the reactor and scour the internal surfaces of the reactor during normal operation. This scouring action reduces the level of fouling on the reactor surfaces. Foulant material (polyethylene) is removed from the process on a continuous basis but the cleaning bodies remain within the reactor. 1. A self cleaning , continuous flow reactor , said reactor comprising1) at least one inlet line for liquid reactants;2) at least one outlet line for liquid products;3) a mixing system to mix liquid contained within said reactor; a) said mixing system provides sufficient liquid velocity to suspend said cleaning bodies within said reactor;', 'b) said cleaning bodies have a particle size of from 2 millimeters to 2 centimeters; and', 'c) said cleaning bodies are retained within said reactor during operation of the reactor., '4) a mass of cleaning bodies contained within said reactor, with the provisos that'}2. The reactor of wherein said reactor is a continuously stirred tank reactor.3. The reactor of wherein said cleaning bodies have a particle size of from about 2 millimeters to about 2 centimeters and a specific gravity that is greater than the specific gravity of said liquid contained within said reactor.4. A process for the removal of by-product polyethylene from a continuous flow claim 1 , mixed claim 1 , oligomerization reactor claim 1 , said process comprising:a) providing input flows comprising ethylene, solvent, and an oligomerization catalyst system to said reactor;b) oligomerizing ethylene under continuous flow conditions within said reactor; andc) providing a discharge stream from said reactor comprising solvent, oligomer product and polyethylene by-product; characterized in that said process is conducted in the presence of a mass ...

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Номер записи: 61
02-06-2022 дата публикации

PROCESS FOR THE CONTINUOUS PRODUCTION OF NITROBENZENE

Номер: US20220169592A1
Автор: DRUMM Christian, Kalem Murat, Knauf Thomas, Racoes Alexandre
Принадлежит:

The invention relates to a continuously operating process for producing nitrobenzene, comprising the following steps: a) nitriding benzene in adiabatic conditions with sulfuric acid and nitric acid, using a stoichiometric excess of benzene in relation to the nitric acid; b) first separating a gaseous phase containing benzene and gaseous secondary components from the raw process product of the nitridation in a gas separator provided specifically for this purpose, then separating, in a downstream phase-separating apparatus, the resulting liquid phase, which is depleted in gaseous components and contains nitrobenzene and sulfuric acid, into a sulfuric acid phase and a nitrobenzene phase; and c) processing the nitrobenzene phase, obtaining nitrobenzene. The invention also relates to a production plant suitable for carrying out the claimed process. 1. A process for the continuous preparation of nitrobenzene , comprising:a) adiabatically reacting a benzene-containing stream a reactor with sulfuric acid and nitric acid using a, based on nitric acid, stoichiometric excess of benzene, to obtain a process product containing nitrobenzene, benzene and sulfuric acid; '(ii) passing the liquid phase produced in step b)(i) into a phase separation apparatus in which the liquid phase is subjected to a phase separation, wherein a liquid aqueous, sulfuric acid-comprising phase and a liquid organic, nitrobenzene-comprising phase are withdrawn from the phase separation apparatus; and', 'b) (i) passing the process product containing nitrobenzene, benzene and sulfuric acid is first passed into a gas separator in which a gaseous phase comprising benzene and gaseous secondary components is removed from the process product, leaving a liquid phase comprising nitrobenzene and sulfuric acid and depleted of gaseous constituents;'}c) working up the liquid organic, nitrobenzene comprising phase to obtain the nitrobenzene.2. The process as claimed in claim 1 , further comprising:d) concentrating the ...

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Номер записи: 62
26-04-2018 дата публикации

PROCESS FOR THE OXIDATION OF STARCH-BASED MATERIALS

Номер: US20180112012A1
Автор: Vezzani Massimo
Принадлежит: Ambiente E Nutrizione S.R.L.

A process for the oxidation of powder materials containing starch, which comprises the successive steps of mixing a powder material comprising starch with an aqueous solution of hydrogen peroxide (HO) and adding to the mixture thus obtained an aqueous solution of ammonia and reacting it with said mixture; the process may also comprise a further step of drying the aforementioned mixture to obtain a powder material containing oxidized starch; the process may advantageously comprise the steps of:—feeding a continuous flow of powder material containing starch into a first reactor (R) comprising a cylindrical tubular body () and a rotor, arranged in the cylindrical tubular body, comprising a shaft () provided with elements () projecting radially therefrom and rotated at a speed greater than or equal to 50 rpm,—feeding into said reactor also a continuous flow of an aqueous solution of hydrogen peroxide—reacting the powder material containing starch and the hydrogen peroxide;—discharging from a discharge opening () of the first reactor a continuous flow of a wet powder and feeding this continuous flow into a second reactor (R′) comprising a cylindrical tubular body () and a rotor, arranged in the cylindrical tubular body, comprising a shaft () provided with elements () projecting radially therefrom and rotated at a speed greater than or equal to 50 rpm;—feeding into the second reactor (R′) also a continuous flow of an aqueous solution of ammonia,—discharging from a discharge opening () of the second reactor a continuous flow of a wet powder comprising oxidized starch;—drying the wet powder to a moisture content less than or equal to 20% by weight, thereby obtaining a powder material containing oxidized starch. 1. A process for the oxidation of powder materials containing starch , which is carried out in the absence of any metal compounds and which comprises the successive steps of:a) providing a powder material comprising starch;{'sub': 2', '2, 'b) mixing said material ...

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Номер записи: 63
09-06-2022 дата публикации

PROCESS FOR PRODUCING TRIFLUOROIODOMETHANE (CF3I) FROM TRIFLUOROACETIC ANHYDRIDE (TFAA)

Номер: US20220177394A1
Автор: NAIR HARIDASAN K., WANG HAIYOU
Принадлежит:

The present disclosure relates to a method for producing trifluoroiodomethane (CFI) from iodine (I) and trifluoroacetic anhydride (TFAA) under photochemical conditions using ultraviolet (UV) light. 1. A method for making trifluoroiodomethane (CFI) comprising:{'sub': '2', 'combining iodine (I) and trifluoroacetic anhydride (TFAA); and'}irradiating the mixture with ultraviolet (UV) light to produce a product stream.2. The method of claim 1 , wherein the combining and irradiating steps are conducted continuously.3. The method of claim 1 , wherein the ratio of iodine (I) to trifluoroacetic anhydride (TFAA) is from about 0.1:1 to about 100:1.4. The method of claim 3 , wherein the ratio of iodine (I) to trifluoroacetic anhydride (TFAA) is from about 10:1 to about 20:15. The method of claim 1 , wherein the ultraviolet (UV) light is broad spectrum ultraviolet (UV) light.6. The method of claim 5 , wherein the broad spectrum ultraviolet light (UV) is 200 nm-400 nm ultraviolet (UV) light.7. The method of claim 1 , wherein the ultraviolet (UV) light is single wavelength ultraviolet (UV) light.8. The method of claim 7 , wherein the ultraviolet (UV) light is 254 nm ultraviolet (UV) light.9. The method of claim 1 , wherein the irradiating step is conducted with the iodine (I) and trifluoroacetic anhydride (TFAA) in the liquid phase.10. The method of claim 1 , further comprising claim 1 , prior to the combining step claim 1 , dissolving the iodine (I) in a solvent.11. The method of claim 10 , wherein the solvent is chosen from the group consisting of mesitylene claim 10 , toluene claim 10 , and xylenes.12. The method of claim 1 , further comprising purifying the product stream.13. The method of claim 1 , wherein the product stream may be passed through two or more cold traps.14. The method of claim 13 , wherein the product stream may be passed through a first cold trap at 0° C.15. The method of claim 13 , wherein the product stream may be passed through a second cold trap at −78° C ...

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Номер записи: 64
18-04-2019 дата публикации

REACTION CHAMBER FOR A CHEMICAL REACTOR, AND CHEMICAL REACTOR CONSTRUCTED THEREFROM

Номер: US20190111406A1
Автор: Boos Karl-Robert, Buchholz Sigurd, FALSS Sebastian, Mleczko Leslaw
Принадлежит:

A reaction chamber for a chemical reactor comprises a casing () of the reaction chamber, a floor () of the reaction chamber having an opening () located in the floor, an agitator shaft () located in the chamber and having at least one agitator element (), connected thereto, wherein the agitator shaft (), seen in the longitudinal direction, has a beginning () and an end (). In the opening () of the floor () a removable sleeve () is provided, which projects out of the reaction chamber. The sleeve () is arranged in alignment with the axis of rotation of the agitator shaft (). The internal diameter of the sleeve () is greater than the diameter of the agitator shaft () and the agitator shaft (), at the beginning () thereof and/or at the end () thereof, is adapted to absorb reversibly a torque provided by means of a further shaft and/or to transmit a torque to a further shaft. Using such a reaction chamber, it is possible to build up modular chemical reactors having decreased backmixing. 2. The process as claimed in claim 1 , wherein the reaction is carried out at least intermittently with a constant amount of substances introduced into the reactor and discharged from the reactor.3. The process as claimed in claim 1 , wherein in the stirred reactor claim 1 , there are arranged following one another claim 1 , a first reaction chamber and a second reaction chamber and the agitator shaft of the first reaction chamber is connected to the agitator shaft of the second reaction chamber to transmit a torque and furthermore at least one operating state is monitored in the first and/or second reaction chamber claim 1 , at a predetermined deviation of the operating state from a predetermined value of this operating state the feeds opening out into this reaction chamber are closed and the substances originally transported through these feeds are introduced into another reaction chamber.4. The process as claimed in claim 3 , wherein the monitored operating state is the pressure drop ...

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Номер записи: 65
18-04-2019 дата публикации

DEVICE FOR CONTINUOUSLY PRODUCING POLY(ARYLENE SULFIDE) AND METHOD FOR CONTINUOUSLY PRODUCING POLY(ARYLENE SULFIDE)

Номер: US20190112426A1
Автор: MIYAHARA MICHIHISA, SAKABE Hiroshi, SUZUKI Kenji
Принадлежит:

Provided are a device for continuously producing poly(arylene sulfide) (hereinafter, referred to as PAS) and a method for continuous PAS production with which resource savings, energy savings, and a reduction in equipment cost are rendered possible. The device for continuous PAS production according to the present invention includes a housing chamber for housing a plurality of reaction cells; wherein the housing chamber is supplied with at least an organic amide solvent, a sulfur source, and a dihalo aromatic compound. In the reaction cells, the sulfur source is polymerized with the dihalo aromatic compound in the organic amide solvent to form a reaction mixture. The reaction cells communicate with each other through a gas phase within the housing chamber. The reaction cells are sequentially connected, and the reaction mixture sequentially moves to each reaction cell. 1. A device for continuously producing poly(arylene sulfide) , the device comprising a housing chamber configured to house a plurality of reaction cells ,the housing chamber being supplied with at least: an organic amide solvent; at least one type of sulfur source selected from the group consisting of hydrogen sulfide, alkali metal sulfides, and alkali metal hydrosulfides; and a dihalo aromatic compound;a reaction mixture being formed by carrying out a polymerization reaction between the sulfur source and the dihalo aromatic compound in the organic amide solvent in at least one or more reaction cells,the reaction cells being mutually communicated through a gas phase within the housing chamber, andthe reaction cells being sequentially connected, and the reaction mixture being sequentially moved to each of the reaction cells.2. The device according to claim 1 , whereinat least one group or more with regard to combinations of adjacent reaction cells are connected in order from the highest maximum liquid surface level of liquid that can be accommodated by the reaction cells, andthe reaction mixture is ...

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Номер записи: 66
16-04-2020 дата публикации

Apparatus and continuous flow process for production of boronic acid derivative

Номер: US20200115393A1
Автор: Andreas Pelz, Christian Schuster, Christopher ZINGANELL, Clemens Stueckler, Maria VASILOIU, Stefan Steinhofer
Принадлежит: Melinta Subsidiary Corp, Melinta Therapeutics Inc

A process for a continuous production of a boronic acid derivative and an apparatus of performing the process are disclosed.

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Номер записи: 67
25-08-2022 дата публикации

Electrochemically recycling a lithium-ion battery

Номер: US20220271356A1
Автор: Lauren E. Crandon, Steven E. Sloop
Принадлежит: Hulico LLC

Examples are disclosed that relate to methods and reactors for recycling a positive electrode material of a lithium-ion battery. One example provides a method of recycling a positive electrode material of a lithium-ion battery. The positive electrode material comprises a metal m having a n+ oxidation state (m n+ ). A reaction mixture is formed comprising the positive electrode material, an oxidizing agent, and lithium ions. The positive electrode material is electrochemically replenished with lithium via electrochemical reduction of the lithium ions while maintaining the n+ oxidation state of the metal m in the positive electrode material via the oxidizing agent.

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Номер записи: 68
02-05-2019 дата публикации

METHOD FOR PRODUCING HYDROCHLOROFLUOROCARBON AND/OR HYDROFLUOROCARBON

Номер: US20190127299A1
Автор: KIDA Shuuzou, NISHITSUJI Masanobu, Takahashi Kazuhiro, TAKAKUWA Tatsuya
Принадлежит: DAIKIN INDUSTRIES, LTD.

Provided is a method for producing HCFC and/or HFC by subjecting a halogenated hydrocarbon and anhydrous hydrogen fluoride to a fluorination reaction in the presence of a catalyst, whereby efficient production can be achieved, without the need to stop the production every time catalytic activity is regenerated or recovered, and without making facilities excessive. Provided as a solution therefor is a method comprising 1. A method for producing hydrochlorofluorocarbon (HCFC) and/or hydrofluorocarbon (HFC) , the method comprising:(A) subjecting a halogenated hydrocarbon to a fluorination reaction using anhydrous hydrogen fluoride in at least two reactors each in the presence of a catalyst to thereby obtain HCFC and/or HFC; and(B) while halting the reaction in at least one of the reactors, obtaining HCFC and/or HFC by the reaction in at least one other reactor.2. The method according to claim 1 , wherein in step (B) claim 1 , catalytic activity is regenerated or recovered in the at least one reactor in which the reaction is halted.3. The method according to claim 1 , further comprising the following step (C):(C) collecting the HCFC and/or HFC obtained in step (A) using a recovering device connected to the at least two reactors.4. The method according to claim 3 , wherein in step (C) claim 3 , a composition containing the HCFC and/or HFC obtained in step (A) is separated from a composition containing an unreacted halogenated hydrocarbon and/or unreacted anhydrous hydrogen fluoride.5. The method according to claim 3 , wherein in step (C) claim 3 , the recovering device is at least one recovering device selected from the group consisting of distillation columns claim 3 , liquid separation devices claim 3 , and flash columns.6. The method according to claim 3 , further comprising the following step (D):(D) recycling the unreacted compounds obtained in step (C) as raw material compounds in the reactors.7. A method for producing HCFC and/or HFC claim 3 , the method ...

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Номер записи: 69
19-05-2016 дата публикации

PLANT AND PROCESS FOR THE EFFICIENT UTILIZATION OF EXCESS ELECTRIC ENERGY

Номер: US20160136608A1
Автор: Böss Florian, Fritsch Swen, Markowz Georg, Neuhaus Raoul
Принадлежит: Evonik Degusssa GmbH

In a plant comprising a first apparatus for the electrochemical or electrothermal production of hydrogen, which produces a first hydrogen stream; a second apparatus for producing hydrogen from a hydrocarbon by steam reforming, partial oxidation or dehydrogenation, which produces a second hydrogen stream; a hydrogen conduit or a hydrogen consumer to which both the first hydrogen stream and the second hydrogen stream are fed; and a control device which matches the production of hydrogen in the first apparatus and in the second apparatus in such a way that the total amount of first hydrogen stream and second hydrogen stream corresponds to a predetermined value, excess electric energy can be efficiently utilized by operating the apparatus for the electrochemical or electrothermal production of hydrogen with excess electric energy. 114-. (canceled)15. A plant for the efficient utilization of excess electric energy , comprising:a) a first apparatus for the electrochemical or electrothermal production of hydrogen, which produces a first hydrogen stream;b) a second apparatus for producing hydrogen from a hydrocarbon by steam reforming, partial oxidation or dehydrogenation, which produces a second hydrogen stream;c) a hydrogen conduit or a hydrogen consumer to which both the first hydrogen stream and the second hydrogen stream are fed; andd) a control device matching the production of hydrogen in the first apparatus and in the second apparatus in such a way that the total amount of first hydrogen stream and second hydrogen stream corresponds to a predetermined value.16. The plant of claim 15 , wherein the second apparatus is an apparatus for the steam reforming of natural gas.17. The plant of claim 15 , wherein the first apparatus is an apparatus for the electrolysis of an aqueous solution to form hydrogen and oxygen.18. The plant of claim 15 , wherein the first apparatus is an apparatus for chloralkali electrolysis.19. The plant of claim 15 , wherein the first apparatus is ...

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Номер записи: 70
03-06-2021 дата публикации

Method for preparing cathode active material precursor for secondary battery, and preparation apparatus using same

Номер: US20210163306A1
Автор: Hwang Yol RYU, Ki Sung YOU
Принадлежит: Posco Co Ltd, Research Institute of Industrial Science and Technology RIST

A method for preparing a cathode active material precursor for a secondary battery, including: moving a co-precipitation filtrate generated after a co-precipitation reaction to a co-precipitation filtrate storage tank; removing a metal hydroxide by passing the co-precipitation filtrate through a filter; reacting the co-precipitation filtrate from which the metal hydroxide is removed with sulfuric acid or nitric acid to produce an ammonium sulfate or an ammonium nitrate while removing ammonia from the co-precipitation filtrate from which the metal hydroxide is removed; cooling and crystallizing the co-precipitation filtrate from which the metal hydroxide and ammonia are removed to precipitate a sodium sulfate; filtering the precipitated sodium sulfate to separate the precipitated sodium sulfate from the co-precipitation filtrate from which the metal hydroxide and ammonia are removed; drying the sodium sulfate separated from the co-precipitation filtrate and moving the co-precipitation filtrate separated from the sodium sulfate to a circulation concentration tank; and heating the co-precipitation filtrate stored in the circulation concentration tank to a predetermined temperature for recycling and performing N2 purging or bubbling, is provided.

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Номер записи: 71
18-05-2017 дата публикации

REACTION CHAMBER FOR A CHEMICAL REACTOR, AND CHEMICAL REACTOR CONSTRUCTED THEREFROM

Номер: US20170136440A1
Автор: Boos Karl-Robert, Buchholz Sigurd, FALSS Sebastian, Mleczko Leslaw
Принадлежит:

A reaction chamber for a chemical reactor comprises a casing () of the reaction chamber, a floor () of the reaction chamber having an opening () located in the floor, an agitator shaft () located in the chamber and having at least one agitator element (), connected thereto, wherein the agitator shaft (), seen in the longitudinal direction, has a beginning () and an end (). In the opening () of the floor () a removable sleeve () is provided, which projects out of the reaction chamber. The sleeve () is arranged in alignment with the axis of rotation of the agitator shaft (). The internal diameter of the sleeve () is greater than the diameter of the agitator shaft () and the agitator shaft (), at the beginning () thereof and/or at the end () thereof, is adapted to absorb reversibly a torque provided by means of a further shaft and/or to transmit a torque to a further shaft. Using such a reaction chamber, it is possible to build up modular chemical reactors having decreased backmixing. 1. A reaction chamber for a chemical reactor , comprising:a casing of the reaction chamber,a floor of the reaction chamber having an opening located in the floor,an agitator shaft located in the chamber and having at least one agitator element, connected thereto, wherein the agitator shaft, seen in the longitudinal direction, has a beginning and an end, whereinin the opening of the floor a removable sleeve is provided, which projects out of the reaction chamber,the sleeve is arranged in alignment with the axis of rotation of the agitator shaft,the internal diameter of the sleeve is greater than the diameter of the agitator shaftand in that the agitator shaft, at the beginning thereof and/or at the end thereof, is adapted to absorb reversibly a torque provided by means of a further shaft and/or to transmit a torque to a further shaft.2. The reaction chamber as claimed in claim 1 , wherein the agitator shaft is conducted out of the reaction chamber through the sleeve in such a manner that ...

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Номер записи: 72
30-04-2020 дата публикации

Method for preparing 2,6-dichloropyridine through liquid phase photochlorination of pyridine

Номер: US20200131128A1
Автор: Huiyue Li, Jiaquan Zhu, Keqiang Jin
Принадлежит: Zhejiang Avilive Chemical Co Ltd

The present invention relates to a method for preparing 2,6-dichloropyridine with product purity greater than or equal to 99.0% by using trifluoromethyl chlorobenzene as a solvent for reaction between pyridine and chlorine gas. The preparation process comprises the following steps: enabling pyridine and chlorine gas to continuously experience chlorination reaction under irradiation of ultraviolet light by using pyridine and chlorine gas as starting materials and using trifluoromethyl chlorobenzene as a solvent, and cooling a chlorination reaction product and the solvent to obtain pyridine chlorination solution. Advantages: firstly, it pioneers the precedent of direct and high-selectivity preparation of 2,6-dichloropyridine through liquid phase photochlorination, and not only can the 2,6-dichloropyridine product with purity greater than or equal to 99.0% be obtained, but also industrial production is facilitated; and secondly, not only can the reuse of the separated solvent in the preparation process of the 2,6-dichloropyridine product with purity greater than or equal to 99.0% be realized, but also the purposes of low pollution, low energy consumption and low cost in the preparation process can be realized.

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Номер записи: 73
16-05-2019 дата публикации

PROCESS FOR A CONTINUOUS SYNTHESIS OF ZEOLITIC MATERIALS

Номер: US20190144290A1
Автор: ARNOLD Lena, CLADE Stefanie, DIEHLMANN Uwe, Marx Stefan, Mueller Ulrich
Принадлежит: BASF SE

The present invention relates to a continuous process for preparing a zeolitic material comprising (i) preparing a mixture comprising a source of YO, optionally a source of XO, and a liquid solvent system; (ii) continuously feeding the mixture prepared in (i) into a continuous flow reactor at a liquid hourly space velocity in the range of from 0.3 to 20 hfor a duration of at least 1 h; and (iii) crystallizing the zeolitic material from the mixture in the continuous flow reactor, wherein the mixture is heated to a temperature in the range of from 100 to 300° C.; wherein the volume of the continuous flow reactor is in the range of from 150 cmto 75 m, as well as to zeolitic materials which may be obtained according to the inventive process and to their use. 1. A continuous process for preparing a zeolitic material , comprising:{'sub': 2', '2', '3, 'preparing a mixture comprising a source of YO, optionally a source of XO, and a liquid solvent system;'}{'sup': '−1', '(ii) continuously feeding the mixture prepared in (i) into a continuous flow reactor at a liquid hourly space velocity in the range of from 0.3 to 20 hfor a duration of at least 1 h; and'}(iii) crystallizing the zeolitic material from the mixture in the continuous flow reactor,wherein the mixture is heated to a temperature in the range of from 100 to 300° C.;{'sup': 3', '3, 'wherein the volume of the continuous flow reactor is in the range of from 150 cmto 75 m.'}2. The process of claim 1 , wherein the continuous flow reactor is selected from the group consisting of a tubular reactor claim 1 , a ring reactor claim 1 , and a continuously oscillating reactor.3. The process of claim 1 , wherein the wall of the continuous flow reactor comprises a metallic material.4. The process of claim 1 , wherein the surface of the inner wall of the continuous flow reactor is lined with an organic polymer material.5. The process of claim 1 , wherein in (iii) the mixture is heated under autogenous pressure.6. The process of ...

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Номер записи: 74
17-06-2021 дата публикации

INTEGRATED PROCESSES FOR PRODUCING BIS(FLUOROSULFONYL) IMIDE

Номер: US20210179428A1
Автор: Luly Matthew H., Pointner Bernard E.
Принадлежит:

A process for producing bis(fluorosulfonyl) imide includes providing a solution comprising fluorosulfonic acid and urea, the solution maintained at a solution temperature from about 0° C. to about 70° C.; reacting the solution in the presence of a reaction medium at a reaction temperature from 80° C. to about 170° C. to produce a product stream including bis(fluorosulfonyl) imide, ammonium fluorosulfate and the reaction medium; separating the ammonium fluorosulfate from the product stream to produce an intermediate product stream; and separating the intermediate product stream into a concentrated product stream and a first recycle stream, the concentrated product stream including a higher concentration of bis(fluorosulfonyl) imide than the first recycle stream. 1. A process for producing bis(fluorosulfonyl) imide , the process comprising:providing a solution comprising fluorosulfonic acid and urea, the solution maintained at a solution temperature from about 0° C. to about 70° C.;reacting the solution in the presence of a reaction medium at a reaction temperature from 80° C. to about 170° C. to produce a product stream including bis(fluorosulfonyl) imide, ammonium fluorosulfate and the reaction medium;separating the ammonium fluorosulfate from the product stream to produce an intermediate product stream; andseparating the intermediate product stream into a concentrated product stream and a first recycle stream, the concentrated product stream including a higher concentration of bis(fluorosulfonyl) imide than the first recycle stream.2. The process of claim 1 , further comprising recycling the first recycle stream back to the reacting step.3. The process of claim 2 , wherein the process is a continuous process.4. The process of claim 1 , further comprising recycling the first recycle stream to a storage tank.5. The process of claim 4 , wherein the process is a semi-batch process.6. The process of claim 1 , wherein the reaction medium includes fluorosulfonic acid.7. ...

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Номер записи: 75
17-06-2021 дата публикации

Process To Produce Distillate From Light Alkanes

Номер: US20210179511A1
Автор: Dakka Jihad M., Wang Kun
Принадлежит:

A method may include reacting at least a naphtha range alkane with oxygen and to produce oxygenate products; reacting at least a portion of the oxygenate products to produce condensed products; and reacting at least a portion of the condensed products with at least hydrogen to produce a distillate range product. 1. A method comprising:reacting at least a naphtha range alkane with oxygen and to produce oxygenate products;reacting at least a portion of the oxygenate products to produce condensed products; andreacting at least a portion of the condensed products with at least hydrogen to produce a distillate range product.2. The method of wherein the step of reacting at least the naphtha range alkane with oxygen comprises reacting the naphtha range alkane in the presence of a boron containing species to produce a boron-oxygenate adduct.3. The method of further comprising hydrolyzing at least a portion of the boron-oxygenate adduct.4. The method of wherein the naphtha range alkane comprises naphtha with carbon numbers ranging from Cto C.5. The method of further comprising at least partially hydrogenating the oxygenate products before the step of reacting at least a portion of the oxygenate products.6. The method of wherein the step of reacting at least a portion of the oxygenate products comprises at least one of dehydrative dimerization claim 1 , aldol condensation claim 1 , Guerbet coupling claim 1 , or a combination thereof.7. The method of wherein the step of reacting at least a portion of the condensed products with hydrogen comprises reacting at least one of olefinic bonds claim 1 , ketones claim 1 , or alcohols present in the condensed products with hydrogen.8. The method of wherein the distillate range product comprises hydrocarbons with carbon numbers ranging from Cto C.9. A method comprising:introducing a naphtha range alkane feed into an oxidation unit wherein the naphtha range alkane feed comprises naphtha with a boiling point of about 30° C. to about 200° C ...

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Номер записи: 76
22-09-2022 дата публикации

DEVICE FOR CONTINUOUSLY PREPARING 2,6-DIHYDROXYBENZALDEHYDE

Номер: US20220297080A1
Автор: FENG Xichun, HONG Hao, LU Jiangping, Yan Bo, Zhang Xin
Принадлежит:

The present disclosure provides a device for continuously preparing 2,6-dihydroxybenzaldehyde and use thereof. The device includes a first continuous reaction unit for hydroxy protection reaction, a second continuous reaction unit for lithiation and hydroformylation, and a third continuous reaction unit for deprotection reaction that are connected in series. The third continuous reaction unit includes: a first columnar continuous reactor, connected to the second continuous reaction unit and used for deprotection of the lithiated hydroformylated product while performing liquid separation to obtain an organic phase containing 2,6-dihydroxybenzaldehyde and an aqueous phase. When the device is applied in the preparation of 2,6-dihydroxybenzaldehyde, reaction time is shortened and the intermediate purification treatment is no longer required. Therefore, compared with batch process, the present disclosure can greatly save equipment cost and post-processing cost, and greatly improve the production efficiency, more beneficial to the industrial scale-up production of 2,6-dihydroxybenzaldehyde. 1. A device for continuously preparing 2 ,6-dihydroxybenzaldehyde , wherein the device comprises a first continuous reaction units , a second continuous reaction unit , and a third continuous reaction unit connected in series , the first continuous reaction units is used for hydroxy protection reaction , the second continuous reaction unit is used for lithiation and hydroformylation , and the third continuous reaction unit is used for deprotection reaction , wherein the third continuous reaction unit comprises:{'b': 32', '20, 'a first columnar continuous reactor (), connected to the second continuous reaction unit () and used for deprotection of the lithiated hydroformylated product while performing liquid separation to obtain an organic phase containing 2,6-dihydroxybenzaldehyde and an aqueous phase.'}2. The device according to claim 1 , wherein the first columnar continuous reactor ...

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Номер записи: 77
07-06-2018 дата публикации

Process for the preparation of a purified acid composition

Номер: US20180155308A1
Автор: Ana Rita Martins Guerreiro Rocha ALMEIDA, Ana Sofia Vagueiro DE SOUSA DIAS, Ines Dacil GONZALEZ JIMENEZ, Martinus Mathilda Pieter Zieverink
Принадлежит: Synvina CV

A purified acid composition including 2,5-furandicarboxylic acid is prepared in a process, including oxidizing a feedstock containing 5-alkoxymethylfurfural to an oxidation product including 2,5-furandicarboxylic acid (FDCA) and 2-formyl-furan-5-carboxylic acid (FFCA), and esters of FDCA and, optionally, esters of FFCA; hydrolyzing the at least part of the oxidation product in the presence of water, thereby hydrolyzing at least esters of FDCA and, optionally, esters of FFCA to obtain an aqueous solution of an acid composition including FDCA, FFCA and ester of FDCA in an amount below the amount of ester of FDCA in the solution of the oxidation product; contacting at least part of the solution of the acid composition with hydrogen in the presence of a hydrogenation catalyst to hydrogenate FFCA to hydrogenation products, yielding a hydrogenated solution; and separating at least a portion of the FDCA from at least part of the hydrogenated solution by crystallization.

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Номер записи: 78
07-06-2018 дата публикации

PROCESS FOR THE PREPARATION OF A PURIFIED ACID COMPOSITION

Номер: US20180155309A1
Автор: Almeida Ana Rita Martins Guerreiro Rocha, de Sousa Dias Ana Sofia Vagueiro, Zieverink Martinus Mathilda Pieter
Принадлежит:

A purified acid composition including 2,5-furandicarboxylic acid is prepared by a process including a) providing an acid composition solution of a crude acid composition in a polar solvent, the crude acid composition including 2,5-furandicarboxylic acid (FDCA) and 2-formyl-furan-5-carboxylic acid (FFCA); b) contacting the acid composition solution with hydrogen in the presence of a hydrogenation catalyst to hydrogenate FFCA to hydrogenation products, such that the hydrogenation products contain a minor amount of 2-methyl-furan-5-carboxylic acid (MFA) or no MFA, yielding a hydrogenated solution; c) separating at least a portion of the FDCA from the hydrogenated solution by crystallization. 1. A process for the preparation of a purified acid composition comprising 2 ,5-furandicarboxylic acid , comprising:a) providing an acid composition solution of a crude acid composition in a polar solvent, the crude acid composition comprising 2,5-furandicarboxylic acid (FDCA) and 2-formyl-furan-5-carboxylic acid (FFCA);b) contacting the acid composition solution with hydrogen in the presence of a hydrogenation catalyst to hydrogenate FFCA to hydrogenation products, such that the hydrogenation products contain up to a minor amount of 2-methyl-furan-5-carboxylic acid (MFA), yielding a hydrogenated solution; andc) separating at least a portion of the FDCA from the hydrogenated solution by crystallization.2. The process according to claim 1 , wherein the acid composition solution is contacted with hydrogen at a temperature in the range of 150 to 200° C. and a contact time with the hydrogenation catalyst in the range of 5 seconds to 15 min.3. The process according to claim 2 , wherein the acid composition solution is contacted with hydrogen at a temperature in the range of 150 to 200° C. and for a contact time with the hydrogenation catalyst of at most 10 min.4. The process according to claim 1 , wherein the hydrogenation catalyst comprises palladium on carbon.5. The process according ...

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Номер записи: 79
07-06-2018 дата публикации

METHOD AND DEVICE FOR MANUFACTURING LACTIDE

Номер: US20180155313A1
Автор: CAVACO MORAO Ana Isabel, DE HAAN André Banier, DE VRIES Johannes Jeichienus
Принадлежит: Purac Biochem BV

A method and a device for manufacturing lactide, whereby crude lactide, being prepared by means of depolymerization of lactic acid oligomers, is purified by means of a distillation step. The prepared crude lactide is maintained for a period of at least 5 hours in a reaction vessel at a temperature between 97° C. and 200° C. prior to the distillation step. Keeping the lactide during a period of time in a reaction vessel leads to a decrease of the lactic acid content and an increase of the lactic acid oligomer concentration, so that the resulting crude lactide can be more efficiently purified during subsequent distillation. A pre-distilling step gives additional advantages. 1. Method for manufacturing lactide , whereby crude lactide , being prepared by means of depolymerization of lactic acid oligomers , is purified by means of a distillation step , wherein , prior to the distillation step , the prepared crude lactide is maintained for a period of at least 5 hours in a reaction vessel at a temperature between 97° C. and 200° C.2. Method according to claim 1 , wherein the crude lactide is maintained for at least 10 hours in the reaction vessel.3. Method according to claim 1 , wherein the reaction vessel is designed as a continuous stirred-tank reactor.4. Method according to claim 3 , wherein the reaction vessel is designed as a series of at least two continuous stirred-tank reactors claim 3 , and that the crude lactide is transported through this series of reactors.5. Method according to claim 1 , wherein the reaction vessel is designed as a plug flow reactor.6. Method according to claim 1 , wherein the crude lactide is maintained in the reaction vessel under ambient pressure.7. Method according to claim 1 , wherein the temperature of the lactide in the reaction vessel(s) ranges between 100° C. and 150° C.8. Method according to claim 1 , wherein a pre-distillation step is performed on the crude lactide between the preparation of the crude lactide and the maintenance of ...

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Номер записи: 80
14-05-2020 дата публикации

Optimized Reactor Configuration for Optimal Performance of the Aromax Catalyst for Aromatics Synthesis

Номер: US20200147573A1
Автор: HASENBERG Daniel M., MCGAHEE Vincent D.
Принадлежит:

A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different. 1. A naphtha reforming reactor system comprising: a plurality of tubes disposed within a reactor furnace,', 'a heat source configured to heat an interior of the reactor furnace; and', 'a naphtha reforming catalyst disposed within the plurality of tubes,', 'wherein at least one tube of the plurality of tubes comprises a graded catalyst bed., 'an isothermal reactor comprising23.-. (canceled)4. The naphtha reforming reactor system of claim 1 , wherein the graded catalyst bed contains a plurality of catalyst zones.5. The naphtha reforming reactor system of claim 4 , wherein the plurality of catalyst zones comprises a first catalyst zone and a second catalyst zone claim 4 , wherein the first catalyst zone is upstream of the second catalyst zone.6. The naphtha reforming reactor system of claim 5 , wherein the first catalyst zone contains a first particle size of the naphtha reforming catalyst claim 5 , wherein the second catalyst zone contains a second particle size of the naphtha reforming catalyst claim 5 , and wherein the first particle size is larger than the second particle size.7. The naphtha reforming reactor system of ...

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Номер записи: 81
23-05-2019 дата публикации

PROCESS FOR MANUFACTURING TETRAFLUOROPROPENE

Номер: US20190152883A1
Автор: Duer-Bert Dominique, Pigamo Anne, Wendlinger Laurent
Принадлежит: Arkema France

A process for manufacturing tetrafluoropropene, including, alternately: at least one step of reacting a chlorinated compound with hydrofluoric acid in the gas phase, in the presence of a fluorination catalyst, the proportion of oxygen optionally present being less than 0.05 mol. % relative to the chlorinated compound; a step of regenerating the fluorination catalyst by bringing the fluorination catalyst into contact with a regeneration stream including an oxidizing agent. Also, equipment suitable for carrying out this process. 1. A plant for the manufacture of tetrafluoropropene , comprising at least one gas-phase fluorination reactor comprising a bed of fluorination catalyst , said gas-phase fluorination reactor being configured in order to be fed alternately by:a system for feeding with reaction stream comprising a chlorinated compound and hydrofluoric acid, the proportion of oxygen optionally present in this reaction stream being less than 0.05 mol % with respect to the chlorinated compound; anda system for feeding with regeneration stream comprising an oxidizing agent.2. The plant as claimed in claim 1 , in which the reaction stream is essentially devoid of oxygen.3. The plant as claimed in claim 1 , in which the regeneration stream contains at least 1 mol % of oxygen with respect to the total regeneration stream.4. The plant as claimed in claim 1 , comprising a single reactor configured in order to be fed alternately by the system for feeding with reaction stream and the system for feeding with regeneration stream.5. The plant as claimed in claim 1 , comprising a plurality of reactors claim 1 , each being configured in order to be fed alternately by a system for feeding with reaction stream and a system for feeding with regeneration stream.6. The plant as claimed in claim 5 , configured so that claim 5 , when a reactor is fed by the system for feeding with reaction stream claim 5 , another reactor is fed by the system for feeding with regeneration stream.7. The ...

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Номер записи: 82
14-06-2018 дата публикации

FLUID-SEGMENTATION DEVICE, FLOW MIXING AND SEGMENTATION DEVICE, CONTINUOUS-FLOW REACTOR SYSTEM, AND METHOD FOR PRODUCING NANOPARTICLES

Номер: US20180161748A1
Автор: Barsic David, Dreilinger Rachel, Haben Patrick Michael, Peterson Daniel
Принадлежит:

The fluid-segmentation device according to an embodiment of the present invention includes: a first conduit in which a first fluid flows, and a second conduit in which a second fluid immiscible with the first fluid flows. The second conduit of the fluid-segmentation device includes an intersection region, to which the first conduit is connected and into which the first fluid is introduced, and a first region downstream of the intersection region. The cross-sectional area of the intersection region of the second conduit in a plane perpendicular to the flow direction of the second fluid is less than the cross-sectional area of the first region of the second conduit in a plane perpendicular to the flow direction of the second fluid. 113-. (canceled)14. A method for producing nanoparticlesby using a second fluid containing precursors of nanoparticles,a first fluid which is immiscible and non-reacting with the second fluid,a first conduit in which the first fluid flows, anda second conduit in which the second fluid flowsby forming a segmented flow of the second fluid, which is separated by intervening segments of the first fluid, and by energizing and/or activating the segmented flow,wherein the second conduit comprises at leasta region of intersection in which the first conduit and the second conduit intersect, anda widening region located downstream of the region of intersection in a flow direction of the second fluid and configured such that a cross-sectional area of the second conduit in a plane perpendicular to the flow direction widens,by introducing the intervening segments of the first fluid from the first conduit to the second conduit to form the segmented flowand by passing the segmented flow through a widening region of the conduit, thereby making the intervening segments of the segmented flow in the flow direction downstream of the widening region shorter than the intervening segments of the segmented flow in the flow direction upstream of the widening region ...

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Номер записи: 83
30-05-2019 дата публикации

Single Step Lactide Production Process with Heat Recovery

Номер: US20190161466A1
Автор: Chaouki Jamal, SELS Bert, Van Wouwe Pieter, YAZDANPANAH Mahdi
Принадлежит:

The present invention relates to a process for synthesizing lactide, comprising the steps of: 115.-. (canceled)16. A process for synthesizing lactide , comprising the steps of:adding thermal energy to at least one of one or more components;providing the one or more components to at least one reactor, the one or more components comprising lactic acid and at least one solvent;converting at least part of the lactic acid into lactide and water;recovering at least part of the lactide;recovering at least part of the at least one solvent;recovering at least part of the thermal energy, wherein at least part of the recovered thermal energy is recovered from the recovered solvent; andadding the recovered thermal energy to at least one of the one or more components.17. The process according to claim 16 , wherein the process is an industrial process for synthesizing lactide claim 16 , and wherein the step of converting at least part of the lactic acid into lactide and water is performed in one step.18. The process according to claim 16 , comprising the step of:recovering at least part of the water;wherein at least part of the recovered thermal energy is recovered from the recovered water.19. The process according to claim 16 , wherein the steps of:recovering at least part of the thermal energy, wherein at least part of the recovered thermal energy is recovered from the recovered solvent; andadding the recovered thermal energy to at least one of the one or more components;are performed with a heat exchanger.20. The process according to claim 16 , wherein at least part of the recovered thermal energy is recovered from the recovered lactide.21. The process to according to claim 16 , wherein the step of recovering at least part of the lactide comprises a first crystallization step and a second crystallization step.22. The process according to claim 16 , wherein the first crystallization step and the second crystallization step are each independently cooled.23. The process according ...

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Номер записи: 84
29-09-2022 дата публикации

CONTINUOUS HYDROLYZATION APPARATUS AND CONTINUOUS HYDROLYZATION METHOD

Номер: US20220306828A1
Автор: Baba Tsuyoshi, Hiraoka Shoko, Hirawaki Satoshi, Ozaki Satoshi
Принадлежит:

A continuous hydrolyzation apparatus includes: a hydrolysis reaction container including a heating tube provided with a feed portion for a hydrolytic resin composition containing fibers and a feed portion for water; a screw inserted in the heating tube and configured to mix the hydrolytic resin composition with the water and to convey a mixture to a downstream side in the heating tube; and a back-pressure valve provided on a downstream side of the hydrolysis reaction container and configured to move the hydrolytic resin composition and the fibers to the downstream side while setting a pressure in the hydrolysis reaction container to a prescribed pressure to promote a hydrolysis reaction. 1. A continuous hydrolyzation apparatus comprising:a hydrolysis reaction container including a heating tube provided with a feed portion for a hydrolytic resin composition containing fibers and a feed portion for water;a screw inserted in the heating tube and configured to mix the hydrolytic resin composition with the water and to convey a mixture to a downstream side in the heating tube; anda back-pressure valve provided on a downstream side of the hydrolysis reaction container and configured to move the hydrolytic resin composition and the fibers to the downstream side while setting a pressure in the hydrolysis reaction container to a prescribed pressure to promote a hydrolysis reaction.2. The continuous hydrolyzation apparatus according to claim 1 ,wherein the back-pressure valve includes a pressure regulation valve configured to maintain an open valve state at a predetermined pressure or above3. The continuous hydrolyzation apparatus according to claim 1 ,wherein the back-pressure valve increases in opening degree in response to a pressure between the hydrolysis reaction container and the back-pressure valve having reached a preset second pressure higher than a first pressure to promote a hydrolysis reaction in the hydrolysis reaction container.4. The continuous hydrolyzation ...

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Номер записи: 85
25-06-2015 дата публикации

HYDROGEN SULFIDE GAS PRODUCTION PLANT SYSTEM AND METHOD FOR RECOVERING AND USING HYDROGEN SULFIDE GAS

Номер: US20150175420A1
Автор: HIROSE Tomoyuki, Matsubara Satoshi, Nakagawa Kouichi, Nakai Osamu, NAKAMURA Masafumi
Принадлежит:

The present invention allows low-concentration hydrogen sulfide gas to be recovered and supplied to a processing plant that uses hydrogen sulfide gas. The hydrogen sulfide gas production plant is provided with a first supply pipe that supplies hydrogen sulfide gas obtained from a sulfur recovery facility to a processing plant, and a second supply pipe that is branched at a predetermined point in the first supply pipe and supplies the hydrogen sulfide gas from the sulfur recovery facility to the processing plant. The first supply pipe has a concentration meter that is provided on the upstream side than the branch point and measures the concentration of the hydrogen sulfide gas. The first supply pipe and the second supply pipe have ON/OFF valves that are provided on the downstream side of the branch point and perform ON/OFF control of the supply to the processing plant through the supply pipe. 1. A hydrogen sulfide gas production plant system , comprising:a plurality of systems of hydrogen sulfide gas production plants provided with at least a reaction facility that generates hydrogen sulfide gas from sulfur and hydrogen gas, a plurality of cooling facilities that cool the generated hydrogen sulfide gas, and a sulfur recovery facility that recovers sulfur contained in the hydrogen sulfide gas,the hydrogen sulfide gas production plant system that:the hydrogen sulfide gas production plant of each system is provided witha first supply pipe that supplies the hydrogen sulfide gas from which sulfur has been recovered in the sulfur recovery facility to a processing plant that uses hydrogen sulfide gas, anda second supply pipe that is branched at a predetermined point in the first supply pipe and supplies the hydrogen sulfide gas from the sulfur recovery facility to the processing plant;the first supply pipe has a concentration meter that is provided on the sulfur recovery facility side than the predetermined branch point and measures the concentration of the hydrogen sulfide ...

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Номер записи: 86
01-07-2021 дата публикации

Extracting desired organic compounds from plants with controlled microwave energy

Номер: US20210197167A1
Автор: Hartz Edwin Lincoln, Hartz Stanley Jay
Принадлежит: DESIRED ORGANIC MICROWAVE EXTRACTION, INC.

Method and system for Improved quality of selected organic compounds extracted from plant material, which may be the whole plant, a selected portion thereof, or combined parts of the plant, by use of one or more adjustable microwave sources in a closed loop from output to input. The selected portions may be the seeds, pods, leaves, stalks or a combination of one or more of the parts. 1. The method of extracting a selected organic compound from plant material comprising the steps of placing the plant material in a processing container , adding water to the plant material in the container and applying pulsed microwave energy to the plant material and water at a frequency and energy level to create a water hammer to open the body of the plant material.2. The method in accordance with comprising the further steps of applying continuous wave microwave energy to the plant material to cause a selected organic compound in the plant material to change phase and extracting this compound.3. The method in accordance with comprising the further steps of cutting up the plant material before placing it in the container.4. The method of further comprising the steps of applying continuous wave microwave energy to the plant material while applying the pulsed microwave energy.5. The method in accordance with wherein the frequency of the pulsed microwave energy is 2.4 to 2.5 GHz.6. The method in accordance with wherein the frequency of the continuous microwave energy is 2.4 to 2.5 GHz.7. A method of extracting organic compounds from plant material comprising the steps of placing the plant material in a container claim 2 , applying continuous wave microwave energy to the plant material to cause the organic compounds in the plant material to change phase and extracting the compounds.8. The method of extracting a selected organic compound from plant material comprising the steps of placing the plant material in a processing container claim 2 , placing the container in a processing chamber ...

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Номер записи: 87
01-07-2021 дата публикации

CONTINUOUS ACOUSTIC CHEMICAL MICROREACTOR

Номер: US20210197168A1
Автор: Farrar Lawrence C., Martineau Zachary Ruprecht, Sperry Grayson
Принадлежит: Resodyn Corporation

A continuous acoustic chemical microreactor system is disclosed. The system includes a continuous process vessel (CPV) and an acoustic agitator coupled to the CPV and configured to agitate the CPV along an oscillation axis. The CPV includes a reactant inlet configured to receive one or more reactants into the CPV, an elongated tube coupled at a first end to the reactant inlet and configured to receive the reactants from the reactant inlet, and a product outlet coupled to a second end of the elongated tube and configured to discharge a product of a chemical reaction among the reactants from the CPV. The acoustic agitator is configured to agitate the CPV along the oscillation axis such that the inner surface of the elongated tube accelerates the one or more reactants in alternating upward and downward directions along the oscillation axis. 1. A method of continuously processing a combination of materials in a chemical microreactor , the method comprising:introducing, via a reactant inlet, one or more reactants into an elongated tube coupled at a first end to the reactant inlet and configured to receive the reactants from the reactant inlet, wherein the elongated tube has an inner surface having a hydraulic diameter of less than 2.5 cm;agitating, using an acoustic agitator coupled to the continuous process vessel, the continuous process vessel along the oscillation axis at a frequency greater than 10 Hz and less than 100 Hz such that the inner surface of the elongated tube accelerates the one or more reactants in alternating upward and downward directions along the oscillation axis; anddischarging, from a product outlet coupled to a second end of the elongated tube, a product of a chemical reaction among the reactants from the continuous process vessel.2. The method of claim 1 , comprising:introducing, via a coolant inlet, a cooling fluid into an interstitial region within the continuous process vessel and surrounding the elongated tube, the interstitial region ...

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Номер записи: 88
23-06-2016 дата публикации

CONTINUOUS SYNTHESIS METHOD FOR A MODIFIED DIENE ELASTOMER, FACILITY FOR IMPLENTING SAME

Номер: US20160176991A1
Автор: DIRE Charlotte, DORATO Margarita, MANCEAU Mathieu, MARECHAL Jean-Mark, PACHECO Nuno
Принадлежит:

A continuous method for synthesizing a diene includes modifying the diene elastomer in a functionalizing device by: 2. The method for the continuous synthesis of a modified diene elastomer according to claim 1 , wherein K is greater than or equal to 10.3. The method according to claim 1 , wherein P is greater than 6.9.5. The method according to claim 4 , wherein X is a function capable of interacting with a reinforcing filler selected from cyclic or non-cyclic claim 4 , primary claim 4 , secondary or tertiary amines claim 4 , isocyanates claim 4 , imines claim 4 , cyano compounds claim 4 , thiols claim 4 , carboxylates claim 4 , epoxides and primary claim 4 , secondary or tertiary phosphines.6. The method according to claim 5 , wherein the function capable of interacting with a reinforcing filler is a secondary amine optionally protected by a trialkylsilyl group or a tertiary amine claim 5 , the nitrogen atom being substituted by C-Calkyl radicals claim 5 , preferably C-Calkyl radicals claim 5 , more preferably a methyl or ethyl radical claim 5 , or else a cyclic amine that forms a heterocycle containing a nitrogen atom and at least one carbon atom claim 5 , preferably 2 to 6 carbon atoms.7. The method according to claim 6 , wherein the functionalizing agent is selected from 3-(N claim 6 ,N-dimethylaminopropyl)trimethoxysilane claim 6 , 3-(N claim 6 ,N-dimethylaminopropyl)triethoxysilane claim 6 , 3-(N claim 6 ,N-diethylaminopropyl)trimethoxysilane claim 6 , 3-(N claim 6 ,N-diethylaminopropyl)-triethoxysilane claim 6 , 3-(N claim 6 ,N-dipropylaminopropyl)trimethoxysilane claim 6 , 3-(N claim 6 ,N-dipropyl-aminopropyl)triethoxysilane claim 6 , 3-(N claim 6 ,N-dibutylaminopropyl)trimethoxysilane claim 6 , 3-(N claim 6 ,N-dibutylaminopropyl)triethoxysilane claim 6 , 3-(N claim 6 ,N-dipentylaminopropyl)trimethoxysilane claim 6 , 3-(N claim 6 ,N-dipentylaminopropyl)triethoxysilane claim 6 , 3-(N claim 6 ,N-dihexylaminopropyl)-trimethoxysilane claim 6 , 3-(N claim 6 ,N- ...

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Номер записи: 89
21-06-2018 дата публикации

DEVICE ALLOWING THE TEMPORARY STORAGE AND PUTTING BACK INTO CIRCULATION OF A CERTAIN QUANTITY OF CATALYST IN CATALYTIC REFORMING INSTALLATIONS

Номер: US20180169601A1
Автор: BANCEL Thierry, FLOER Cecile, LAMBERT Fabian, RICHARD Florence, VINAY Guillaume
Принадлежит: IFP ENERGIES NOUVELLES

The present invention describes a device that firstly allows temporary storage of a certain quantity of catalyst and, secondly, the putting back into circulation of said quantity in the regenerative reforming installations following an interruption in the circulation of the catalyst. 153532575711257715. Catalytic reactor implementing a ring-shaped moving bed catalyst , limited at its outer periphery by walls forming a cylindrical basket () , and at its internal periphery by a central collector () , with the catalyst flowing slowly by force of gravity into the space between the basket () and the central collector () , and circulating downwards through circulation legs () positioned on the substantially hemispherical base of said reactor , said baskets being movable along a substantially vertical axis over a distance of from a few centimetres to 10 cm , this basket () being equipped with flaps () themselves substantially vertical , positioned on the lower part of the basket () , in the extension of the wall of said flap () , in which reactor , when there is an interruption in the circulation of the catalyst , a catalyst storage space () situated in the lower part of the reactor adjoining the wall , and close to the dip legs () , is released by moving the basket () and attached flaps () assembly upwards , the flap () itself being equipped with a deflector () rigidly or freely attached , and which forms an angle alpha with the vertical of between 30 and 60° , preferably of between 45 and 55°.2157. Catalytic reactor according to claim 1 , wherein the deflector () is rigidly connected to the flap ().31115. Catalytic reactor according to claim 1 , wherein the catalyst is put back into circulation by gravity as soon as circulation has been re-established claim 1 , with the storage area () progressively emptying itself of the catalyst by means of the deflector ().45553. Moving bed catalytic reactor according to claim 1 , in which the catalyst is enclosed in ring-shaped ...

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Номер записи: 90
21-06-2018 дата публикации

Process for the Preparation of Intermediates Useful in the Preparation of Non-ionic Contrast Agents

Номер: US20180169607A1
Автор: Bazinet Patrick R., Heggie William, Naber John, Tomas Filipe
Принадлежит: Hovione Scientia Limited

The invention relates to a process for the preparation of one or more intermediate chemical compounds useful in the preparation of non-ionic contrast agents wherein the process is carried out continuously using one or more flow procedures. 1. A process for the preparation of one or more intermediate chemical compounds useful in the preparation of non-ionic contrast agents wherein the process is carried out continuously using one or more flow procedures.2. A process according to claim 1 , wherein the one or more flow procedures comprise the use of one or more continuous flow reactors.3. A process according to or claim 1 , wherein the one or more continuous flow reactors comprises a pipe reactor claim 1 , a plug flow reactor claim 1 , a tube reactor claim 1 , a piston flow reactor or another commercially available continuous flow reactor claim 1 , or a combination of two or more such reactors.4. A process according to claim 1 , or claim 1 , wherein the process comprises a multi-step chemical synthesis comprising two or more sequential chemical reactions claim 1 , each reaction leading to the production of an intermediate chemical compound useful in the preparation of non-ionic contrast agents or wherein at least two intermediate chemical compounds useful in the preparation of non-ionic contrast agents are prepared in sequence.5. A process according to claim 4 , wherein one or more reactions is carried out in a continuous flow reactor.6. A process according to claim 5 , wherein all of the reactions are carried out in the one or more continuous flow reactors.7. A process according to or claim 5 , wherein each reaction is carried out in a separate continuous flow reactor.8. A process according to any preceding claim claim 5 , wherein an intermediate chemical compound resulting from the process is used to prepare a non-ionic contrast agent.9. A process according to any preceding claim claim 5 , wherein the process comprises at least two chemical reaction steps carried out ...

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Номер записи: 91
21-06-2018 дата публикации

Parallel Reactor System for Ethylbenzene Dehydrogenation

Номер: US20180170836A1
Автор: Clark Jason, Pelati Joseph E
Принадлежит:

A multi-stage dehydrogenation process including contacting, in a first stage, a feed stream comprising a hydrocarbon and steam with a dehydrogenation catalyst under dehydrogenation conditions to yield a first stage effluent, heating the first stage effluent, and contacting, in a second stage, the heated first stage effluent with a dehydrogenation catalyst under dehydrogenation conditions to yield a second stage effluent comprising a dehydrogenation product, wherein the first stage includes a first reactor and a second reactor arranged in parallel, and wherein the second stage includes a third reactor connected in series with the first reactor and the second reactor. A multi-stage dehydrogenation system for carrying out dehydrogenation is also provided. 1. A multi-stage dehydrogenation process comprising:contacting, in a first stage, a feed stream comprising a hydrocarbon and steam with a dehydrogenation catalyst under dehydrogenation conditions to yield a first stage effluent;heating the first stage effluent; andcontacting, in a second stage, the heated first stage effluent with a dehydrogenation catalyst under dehydrogenation conditions to yield a second stage effluent comprising a dehydrogenation product,wherein the first stage includes a first reactor and a second reactor arranged in parallel, andwherein the second stage includes a third reactor connected in series with the first reactor and the second reactor.2. The process of claim 1 , wherein contacting the feed stream in the first stage comprises:contacting a first portion of the feed stream with the dehydrogenation catalyst in the first reactor to yield a first reactor effluent; andcontacting a second portion of the feed stream with the dehydrogenation catalyst in the second reactor to yield a second reactor effluent.3. The process of claim 2 , further comprising:combining the first reactor effluent and the second reactor effluent to form the first stage effluent prior to the step of heating.4. The process ...

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Номер записи: 92
22-06-2017 дата публикации

Process for producing nitrobenzene

Номер: US20170174612A1
Автор: Peter Drinda, Thomas Knauf
Принадлежит: Covestro Deutschland AG

The present invention relates to a process for the continuous production of nitrobenzene by the nitration of benzene with nitric acid and sulphuric acid under adiabatic conditions, not the entire production plant being shut down during a production stop, but the production plant being entirely or at least partly operated in recirculation mode. The invention further relates to a plant for producing nitrobenzene and to a method for operating a plant for producing nitrobenzene.

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Номер записи: 93
06-06-2019 дата публикации

Single Step Lactide Production Process with Hydrolysis of Oligomers and Catalyst by Recovered Water

Номер: US20190169155A1
Автор: Chaouki Jamal, SELS Bert, Van Wouwe Pieter, YAZDANPANAH Mahdi
Принадлежит:

The present invention relates to a process for synthesizing lactide comprising the steps of: 115.-. (canceled)17. The process according to claim 16 , wherein the process is an industrial process for synthesizing lactide.18. The process according to claim 16 , wherein the one or more components provided to the at least one reactor comprises at least 1% by weight of lactic acid and at most 95% by weight of lactic acid claim 16 , with % by weight based on the total weight of the one or more components.19. The process according to claim 16 , wherein the step of converting at least part of the lactic acid oligomers in the mixture into lactic acid and into lactic acid dimer is performed through hydrolysis by the recovered water and/or through hydrolysis by water present in the feed.20. The process according to claim 16 , wherein the one or more components comprise at least one catalyst system claim 16 , and wherein the process comprises the steps of:providing at least one catalyst system to the at least one reactor;recovering at least part of the at least one catalyst system; andregenerating at least part of the recovered catalyst system.21. The process according to claim 20 , wherein the step of regenerating at least part of the recovered catalyst system is performed through hydrolysis by the recovered water and/or through hydrolysis by water present in the feed.22. The process according to claim 20 , wherein the at least one catalyst system is regenerated in-line with the at least one reactor.23. The process according to claim 20 , wherein the at least one catalyst system comprises an acidic zeolite.24. The process according to claim 16 , wherein the step of removing at least part of the water from the mixture is performed with a membrane.25. The process according to claim 16 , wherein the feed comprises lactic acid oligomers.26. The process according to claim 16 , wherein the feed comprises at least 1% by weight lactic acid oligomers and at most 20% by weight lactic ...

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Номер записи: 94
06-06-2019 дата публикации

Single Step Lactide Production Process with Separate Entry for Solvent

Номер: US20190169156A1
Автор: Chaouki Jamal, SELS Bert, Van Wouwe Pieter, YAZDANPANAH Mahdi
Принадлежит:

The present invention relates to a process for synthesizing lactide, comprising the steps of: 115.-. (canceled)17. The process according to claim 16 , wherein the process is an industrial process for synthesizing lactide.18. The process according to claim 16 , wherein prior to the step of adding the at least one solvent to the at least one reactor claim 16 , the solvent has a temperature of at least 140° C. and at most 300° C.19. The process according to claim 16 , wherein prior to the step of adding the at least one solvent to the at least one reactor claim 16 , the solvent has a temperature of at least 5° C. and at most 100° C. greater than the temperature of the lactic acid.20. The process according to claim 16 , wherein the one or more components are provided to at least two reactors.21. The process according to claim 20 , comprising the step of recovering at least part of the water claim 20 , wherein the at least part of the water is recovered between the at least two reactors.22. The process according to claim 21 , wherein at least 50% of the water is recovered between the at least two reactors claim 21 , based on the total amount of water exiting the first reactor of the at least two reactors.23. The process according to claim 20 , wherein the at least one solvent is divided into at least two solvent fractions claim 20 , and wherein each solvent fraction is separately provided to each reactor of the at least two reactors.24. The process according to claim 23 , wherein the at least two solvent fractions comprise a first solvent fraction and a second solvent fraction claim 23 , and wherein at least part of the thermal energy is added to the first solvent fraction.25. The process according to claim 24 , wherein the at least two solvent fractions comprise a first solvent fraction and a second solvent fraction claim 24 , and wherein at least part of the thermal energy is added to the second solvent fraction.27. The process according to claim 16 , wherein the ...

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Номер записи: 95
28-05-2020 дата публикации

CONTINUOUS MANUFACTURE OF GUIDANCE MOLECULE DRUG CONJUGATES

Номер: US20200164338A1
Автор: COTTFRIED Michael, Kaiser Klaus, KRUEGER Joachim, LINGEN Verena, Paulsen Holger
Принадлежит:

Described herein is a modification unit () for the continuous, pathogen reduced processing of a guidance molecule e.g. a conjugate of a peptide or a protein or a nucleic acid and a linker comprising the following components: 1. Modification unit for continuous , pathogen reduced processing of a guidance molecule , optionally a peptide or a protein or a nucleic acid and a linker comprising the following components:at least one reservoir containing the guidance molecule in buffer solution and/or at least one inlet for a product stream containing the guidance molecule in buffer solution,at least one reservoir containing the linker in solution,at least one mixing device,at least two valves, one for dosage of the guidance molecule and one for dosage of the linker moleculeat least one outlet for the product stream comprising the guidance molecule-linker complexes and/or a reservoir for taking up the guidance molecule-linker complexes andfurther comprising at least one residence time device ensuring a defined residence time, optionally ensuring that after mixing the guidance molecules and the linker molecules always spend a similar amount of time in a continuous process.2. Modification unit according to claim 1 , further comprising at least three valves.3. Modification unit according to claim 1 , wherein the residence time device is a CFI or a HFI.4. Modification unit according to claim 1 , wherein the guidance molecule is a protein and said protein is an antibody.5. Modification unit according to claim 1 , further comprising at least one pump.6. Modification unit for continuous claim 1 , pathogen reduced processing of a guidance molecule claim 1 , optionally a peptide or a protein or a nucleic acid and a linker comprising the following components:at least one reservoir containing the guidance molecule in buffer solution and/or at least one inlet for a product stream containing the guidance molecule in buffer solution,at least one reservoir containing the linker in ...

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Номер записи: 96
08-07-2021 дата публикации

CONTINUOUS TUBULAR REACTOR AND METHOD OF OPERATING THE SAME

Номер: US20210205777A1
Автор: Baek Changyeon, Hyun Gahee, JUNG Won Sik, KIM Hyojin, Kim Jin Seong
Принадлежит:

A continuous tubular reactor includes a rotary reaction tube having a reactant inlet and a product outlet, and including a ceramic; a heating device disposed outside the rotary reaction tube; and an angle adjuster adjusting an angle of a rotation axis of the rotary reaction tube. The angle of the rotation axis is 75° or less with respect to a horizontal surface. 1. A continuous tubular reactor , comprising:a rotary reaction tube having a reactant inlet and a product outlet, and including a ceramic;a heating device disposed outside the rotary reaction tube; andan angle adjuster adjusting an angle of a rotation axis of the rotary reaction tube.2. The continuous tubular reactor of claim 1 , wherein the angle of the rotation axis is 75° or less with respect to a horizontal surface.3. The continuous tubular reactor of claim 1 , wherein the rotary reaction tube comprises one or more selected from a group consisting of an oxide-based ceramic claim 1 , a nitride-based ceramic claim 1 , a carbide-based ceramic claim 1 , a fluoride-based ceramic and a boride-based ceramic.4. The continuous tubular reactor of claim 1 , wherein a blade is disposed on an inner wall of the rotary reaction tube.5. The continuous tubular reactor of claim 4 , wherein a ratio (h/r) of a height h of the blade to a radius r of an inner diameter of the rotary reaction tube is in a range of 0.01 or more and 0.5 or less.6. The continuous tubular reactor of claim 4 , wherein the blade is disposed in a direction parallel to a rotation axis of the rotary reaction tube.7. The continuous tubular reactor of claim 4 , wherein the blade is disposed in a direction perpendicular to a rotation axis of the rotary reaction tube.8. The continuous tubular reactor of claim 4 , wherein the blade is disposed in a spiral direction with respect to a rotation axis of the rotary reaction tube.9. The continuous tubular reactor of claim 1 , wherein a plurality of blades are disposed on an inner wall of the rotary reaction tube. ...

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Номер записи: 97
08-07-2021 дата публикации

Renewable Diesel Fuel Production in Retrofitted Fossil Petroleum Refinery to Produce Biiofuel and Bio-Feedstock for Steam Crackers

Номер: US20210207038A1
Автор: Vermeiren Walter
Принадлежит:

The present invention relates to a process for the conversion of a feedstock comprising at least 50 wt % related to the total weight of the feedstock of triglycerides, fatty acid esters and/or fatty acids having at least 10 carbon atoms into hydrogen, olefins, dienes, aromatics, gasoline, diesel fuel, jet fuel, naphtha and liquefied petroleum gas comprising: 112.-. (canceled)14. The process according to wherein the first and second reactors are existing units used and wherein the process is obtained from the retrofit of an existing plant.15. The process according to wherein the feedstock comprises at least 25 wt % of triglycerides claim 13 , fatty acid esters and/or fatty acids related to the total weight of the feedstock.16. The process according to wherein hydrogen used in step a) is supplied from a naphtha reformer claim 13 , steam cracker being the steam cracker of step c) or steam methane reformer.17. The process according to wherein in step c) the sum of hydrogen claim 13 , ethylene claim 13 , propylene claim 13 , butadiene and benzene produced on the steam cracker originating from the first stream is at least 60 wt % of the converted first stream.18. The process according to wherein the naphtha or liquefied petroleum gas or any mixture thereof produced in step d) are mixed with the first stream of step c) before being sent to the steam cracker of step c).19. The process according to wherein the triglycerides claim 13 , fatty acids esters and/or fatty acids contained in the feedstock are obtained by at least one of the following purification steps:Chemical refining, physical refining, including degumming, bleaching, steam distillation or vacuum distillation, of fats and oils, orhydrolysis of triglycerides of fats and oils, to obtain glycerol and a mixture of free fatty acids.20. The process according to wherein the hydrodesulfurization catalyst is selected among Ni claim 13 , Mo claim 13 , W claim 13 , Co or mixtures like NiW claim 13 , NiMo claim 13 , CoMo ...

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Номер записи: 98
13-06-2019 дата публикации

HIGH-PRESSURE POLYMERIZATION PROCESS OF ETHYLENICALLY UNSATURATED MONOMERS IN A PRODUCTION LINE HAVING FLANGES COVERED BY A CHIMNEY CONSTRUCTION

Номер: US20190177447A1
Автор: Finette Andre-Armand, Gonioukh Andrei, Herrmann Thomas, Littmann Dieter, Wolfram Sven
Принадлежит: BASELL POLYOLEFINE GMBH

A process for polymerizing or copolymerizing ethylenically unsaturated monomers at pressures in the range of from 110 MPa to 500 MPa in a production line comprising a continuously operated polymerization reactor, wherein at least one of a pre-heater or pre-cooler, a polymerization reactor or a post reactor cooler is composed of tubes of a length from 5 m to 25 m which are flanged together, either directly or via bends, and the flanges are covered by a chimney construction, and wherein air is conveyed through the chimney construction and the air exiting the chimney construction is monitored with respect to the hydrocarbons concentration. 1. A process for polymerizing or copolymerizing one or more ethylenically unsaturated monomers at temperatures from 100° C. to 350° C. and pressures in the range of from 110 MPa to 500 MPa in a continuously operated polymerization reactor ,wherein the polymerization is carried out in a production line in which the monomers are brought to the polymerization pressure by one or more compressors in a sequence of compression stages in which the compressed gas mixture is cooled after each compression stage by a compression stage cooler, the compressed monomers are optionally passed through a pre-heater or a pre-cooler and transferred into the polymerization reactor, which is optionally cooled by cooling jackets, a reaction mixture obtained by the polymerization is leaving the reactor through a pressure control valve, and optionally cooled by an post reactor cooler, the reaction mixture is separated into polymeric and gaseous components in two or more stages, where the gaseous components separated off in a first stage at an absolute pressure of from 15 MPa to 50 MPa are recycled to the one or more compressors via a high-pressure gas recycle line, and the gaseous components separated off in a second stage at an absolute pressure in the range of from 0.1 to 0.5 MPa are recycled to the first stage of the sequence of compression stages via a ...

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Номер записи: 99
15-07-2021 дата публикации

CONTINUOUS PREPARATION OF AN OPTICALLY ACTIVE CARBONYL COMPOUND BY ASYMMETRIC HYDROGENATION

Номер: US20210214296A1
Автор: Bey Oliver, Zehner Peter
Принадлежит:

Process for the continuous production of an optically active carbonyl compound by asymmetric hydrogenation of a prochiral α,β-unsaturated carbonyl compound with hydrogen in the presence of a homogeneous rhodium catalyst that has at least one chiral ligand, wherein a liquid reaction mixture comprising the prochiral α,β-unsaturated carbonyl compound is subjected in a first, backmixed reactor to a gas/liquid two-phase hydrogenation, and the liquid reaction mixture is then further hydrogenated in a second reactor, wherein the prochiral α,β-unsaturated carbonyl compound is employed in the first reactor in a concentration from 3% to 20% by weight. The process allows a high total conversion to the prochiral α,β-unsaturated carbonyl compound. 1. A process for the continuous production of an optically active carbonyl compound by asymmetric hydrogenation of a prochiral α ,β-unsaturated carbonyl compound with hydrogen in the presence of a homogeneous rhodium catalyst that has at least one chiral ligand , whereina liquid reaction mixture comprising the prochiral α,β-unsaturated carbonyl compound is subjected in a first, backmixed reactor to a gas/liquid two-phase hydrogenation, andthe liquid reaction mixture is then further hydrogenated in a second reactor,wherein the prochiral α,β-unsaturated carbonyl compound is employed in the first reactor in a concentration from 3% to 20% by weight.2. The process according to claim 1 , wherein hydrogen gas undergoes dispersion in the liquid reaction mixture in a section of the second reactor located at the entrance to the second reactor.3. The process according to claim 1 , wherein the prochiral α claim 1 ,β-unsaturated carbonyl compound is employed in the first reactor in a concentration at which the reaction rate is at least 0.8 times V claim 1 , Vbeing the maximum value for the reaction rate in a plot of the reaction rate against the concentration of the prochiral α claim 1 ,β-unsaturated carbonyl compound.4. The process according to ...

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Номер записи: 100