RU2010139275A - Способ проведения синтеза фишера-тропша и реактор для его осуществления - Google Patents
Способ проведения синтеза фишера-тропша и реактор для его осуществления Download PDFInfo
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- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
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- C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
- C07C31/02—Monohydroxylic acyclic alcohols
- C07C31/04—Methanol
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- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00123—Fingers
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/0015—Plates; Cylinders
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
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- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00761—Details of the reactor
- B01J2219/00763—Baffles
- B01J2219/00765—Baffles attached to the reactor wall
- B01J2219/0077—Baffles attached to the reactor wall inclined
- B01J2219/00772—Baffles attached to the reactor wall inclined in a helix
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
1. Способ проведения синтеза Фишера-Тропша (ФТ), включающий стадии реакции синтез-газа, содержащего водород, монооксид углерода и диоксид углерода, в реакторе с неподвижным слоем частиц катализатора для синтеза ФТ, косвенно охлаждаемых посредством охлаждающего агента, и конденсации воды по мере ее образования на охлаждающей поверхности путем регулирования давления охлаждающего агента с обеспечением точки кипения (TBW) охлаждающего агента в интервале между 50°С и 190°С. ! 2. Способ проведения синтеза Фишера-Тропша (ФТ), включающий стадии реакции синтез-газа, содержащего водород, монооксид углерода и диоксид углерода, в реакторе с неподвижным слоем частиц катализатора для синтеза ФТ, косвенно охлаждаемых посредством охлаждающего агента, и конденсации воды по мере ее образования на охлаждающей поверхности путем регулирования температуры жидкого охлаждающего агента в интервале между 50°С и 190°С. ! 3. Способ по п.1 или 2, отличающийся тем, что, по меньшей мере, часть температуры катализатора поддерживают на уровне выше точки росы воды путем регулирования площади охлаждающей поверхности (ACOOL) при заданной точке кипения охлаждающего агента с обеспечением соотношения объема заданной осевшей массы катализатора к площади охлаждающей поверхности в интервале между 0,01 м и 0,125 м. ! 4. Способ по п.3, отличающийся тем, что температуру частиц катализатора для синтеза ФТ поддерживают на уровне выше точки росы воды посредством нагревающего агента, включающего воду под давлением с точкой кипения между 180°С и 280°С, пар с точкой росы между 180°С и 280°С, или их смесь, причем нагревающий агент пропускают через внутреннее нагревательное средс�
Claims (9)
1. Способ проведения синтеза Фишера-Тропша (ФТ), включающий стадии реакции синтез-газа, содержащего водород, монооксид углерода и диоксид углерода, в реакторе с неподвижным слоем частиц катализатора для синтеза ФТ, косвенно охлаждаемых посредством охлаждающего агента, и конденсации воды по мере ее образования на охлаждающей поверхности путем регулирования давления охлаждающего агента с обеспечением точки кипения (TBW) охлаждающего агента в интервале между 50°С и 190°С.
2. Способ проведения синтеза Фишера-Тропша (ФТ), включающий стадии реакции синтез-газа, содержащего водород, монооксид углерода и диоксид углерода, в реакторе с неподвижным слоем частиц катализатора для синтеза ФТ, косвенно охлаждаемых посредством охлаждающего агента, и конденсации воды по мере ее образования на охлаждающей поверхности путем регулирования температуры жидкого охлаждающего агента в интервале между 50°С и 190°С.
3. Способ по п.1 или 2, отличающийся тем, что, по меньшей мере, часть температуры катализатора поддерживают на уровне выше точки росы воды путем регулирования площади охлаждающей поверхности (ACOOL) при заданной точке кипения охлаждающего агента с обеспечением соотношения объема заданной осевшей массы катализатора к площади охлаждающей поверхности в интервале между 0,01 м и 0,125 м.
4. Способ по п.3, отличающийся тем, что температуру частиц катализатора для синтеза ФТ поддерживают на уровне выше точки росы воды посредством нагревающего агента, включающего воду под давлением с точкой кипения между 180°С и 280°С, пар с точкой росы между 180°С и 280°С, или их смесь, причем нагревающий агент пропускают через внутреннее нагревательное средство, площадь поверхности которого выбрана с обеспечением соотношения площади нагревательного средства к площади поверхности охлаждающего средства в интервале между 0,3 и 3,0.
5. Способ по п.1, отличающийся тем, что точка кипения охлаждающего агента находится в интервале между 100°С и 180°С, и соотношение объема осевшей массы катализатора (VCAT) к площади охлаждающей поверхности (ACOOL) составляет от 0,01 м до 0,125 м.
6. Способ по п.2, отличающийся тем, что средняя температура жидкого охлаждающего агента находится в интервале между 100°С и 180°С, и соотношение объема осевшей массы катализатора (VCAT) к площади охлаждающей поверхности (ACOOL) составляет от 0,01 м до 0,125 м.
7. Реактор для синтеза ФТ для осуществления способа по п.1 или 2, содержащий неподвижный слой частиц катализатора для синтеза ФТ и средство охлаждения, выполненное с возможностью косвенного охлаждения синтез-газа ФТ с помощью охлаждающего агента, размещенные в общем корпусе, причем соотношение объема осевшей массы катализатора к площади охлаждающей поверхности (VCAT/ACOOL) охлаждающего средства составляет от 0,01 м до 0,125 м.
8. Реактор для синтеза ФТ для осуществления способа по п.4, содержащий неподвижный слой частиц катализатора для производства метанола, средство охлаждения, выполненное с возможностью косвенного охлаждения синтез-газа ФТ с помощью охлаждающего агента, и нагревательное средство, выполненное с возможностью косвенного поддержания температуры катализатора для синтеза ФТ с помощью нагревающего агента, размещенные в общем корпусе, причем соотношение площади поверхности нагревательного средства к площади поверхности охлаждающего средства (VCAT/ACOOL) составляет от 0,3 до 3,0.
9. Реактор для синтеза ФТ по п.7 или 8, содержащий дополнительно внутреннее средство для стабилизации жидкой пленки, смежное с поверхностью средства охлаждения.
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Application Number | Priority Date | Filing Date | Title |
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DKPA200800261 | 2008-02-25 | ||
DKPA200800260 | 2008-02-25 | ||
DKPA200800260 | 2008-02-25 | ||
DKPA200800261 | 2008-02-25 | ||
DKPA200800652 | 2008-05-08 | ||
DKPA200800652 | 2008-05-08 | ||
PCT/EP2009/000973 WO2009118080A1 (en) | 2008-02-25 | 2009-02-12 | Method and reactor for performing fischer-tropsch synthesis |
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RU2010139275A true RU2010139275A (ru) | 2012-04-10 |
RU2481151C2 RU2481151C2 (ru) | 2013-05-10 |
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US (3) | US8202915B2 (ru) |
EP (3) | EP2249958B1 (ru) |
JP (2) | JP2011515333A (ru) |
KR (2) | KR20100138884A (ru) |
CN (2) | CN101959586B (ru) |
AT (2) | ATE521407T1 (ru) |
AU (2) | AU2009218827B2 (ru) |
BR (2) | BRPI0906447B1 (ru) |
CA (2) | CA2713874C (ru) |
EA (2) | EA019311B1 (ru) |
ES (3) | ES2368027T3 (ru) |
MX (2) | MX2010008947A (ru) |
NZ (2) | NZ587453A (ru) |
PL (3) | PL2374533T3 (ru) |
RU (1) | RU2481151C2 (ru) |
WO (2) | WO2009106232A1 (ru) |
ZA (2) | ZA201004473B (ru) |
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PL2571612T3 (pl) | 2010-05-20 | 2015-05-29 | Haldor Topsoe As | Sposób oraz urządzenie do oddzielania cieczy od strumienia gazu wsadowego w reaktorze katalitycznym |
CA2802941C (en) | 2010-06-24 | 2017-02-21 | Haldor Topsoe A/S | Co-production of methanol and ammonia |
US20130153188A1 (en) * | 2011-12-16 | 2013-06-20 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Advanced smr reactor design featuring high thermal efficiency |
EP3034161A1 (en) * | 2014-12-18 | 2016-06-22 | Haldor Topsøe A/S | Method and reactor design for the production of methanol |
DE102015202680A1 (de) | 2015-02-13 | 2016-08-18 | Friedrich-Alexander-Universität Erlangen-Nürnberg | Verfahren zur Durchführung einer chemischen Synthese und Synthesereaktor |
WO2017009050A1 (en) * | 2015-07-15 | 2017-01-19 | Haldor Topsoe A/S | Catalytic reactor |
US20180214837A1 (en) * | 2015-07-29 | 2018-08-02 | Primus Green Energy Inc. | Two-stage reactor for exothermal and reversible reactions and methods thereof |
WO2017118572A1 (en) | 2016-01-07 | 2017-07-13 | Total Research & Technology Feluy | Supported indium oxide catalyst and process for methanol synthesis using the same |
DK3400099T3 (da) | 2016-01-07 | 2020-06-02 | Total Raffinage Chimie | Fremgangsmåde til methanolsyntese under anvendelse af en indiumoxidbaseret katalysator |
CN105797653A (zh) * | 2016-03-19 | 2016-07-27 | 江苏怡达化学股份有限公司 | 直接氧化法制备环氧丙烷的绿色合成反应装置及工艺 |
DE102016204717A1 (de) | 2016-03-22 | 2017-09-28 | Siemens Aktiengesellschaft | Reaktor zur Durchführung von gleichgewichtslimitierten Reaktionen |
DE102016204718A1 (de) | 2016-03-22 | 2017-09-28 | Siemens Aktiengesellschaft | Reaktor |
US10478798B2 (en) | 2016-03-30 | 2019-11-19 | Haldor Topsoe A/S | Methanol synthesis process layout for large production capacity |
EP3401300B1 (de) * | 2017-05-12 | 2021-06-23 | L'air Liquide, Société Anonyme Pour L'Étude Et L'exploitation Des Procédés Georges Claude | Verfahren zur herstellung von methanol |
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