RU2013124424A - Одноконтурное многоступенчатое получение топлива - Google Patents
Одноконтурное многоступенчатое получение топлива Download PDFInfo
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- RU2013124424A RU2013124424A RU2013124424/04A RU2013124424A RU2013124424A RU 2013124424 A RU2013124424 A RU 2013124424A RU 2013124424/04 A RU2013124424/04 A RU 2013124424/04A RU 2013124424 A RU2013124424 A RU 2013124424A RU 2013124424 A RU2013124424 A RU 2013124424A
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- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
- C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
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- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/72—Copper
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
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- 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
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- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
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- C07C41/09—Preparation of ethers by dehydration of compounds containing hydroxy groups
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- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
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- C10G2/332—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals of the iron-group
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- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
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- C10G3/46—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof in combination with chromium, molybdenum, tungsten metals or compounds thereof
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- C10G3/48—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support
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- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
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- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- Materials Engineering (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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Abstract
1. Способ получения топлива из синтез-газа, включающий стадии:а) пропускания синтез-газа через первый реактор с целью конверсии синтез-газа в метанол и воду с образованием первого выходящего потока,б) пропускания первого выходящего потока через второй реактор с целью конверсии метанола в простой диметиловый эфир с образованием второго выходящего потока,в) пропускания второго выходящего потока через третий реактор с целью конверсии метанола и простого диметилового эфира в топливо и тяжелый бензин с образованием третьего выходящего потока,г) пропускания третьего выходящего потока через четвертый реактор с целью конверсии тяжелого бензина в изопарафины, нафтены и ароматические соединения с низкой степенью замещения с образованием четвертого выходящего потока, ид) возвращения непрореагировавшего синтез-газа, содержащегося в четвертом выходящем потоке, в повторный цикл в первый реактор,причем на протяжении способа не осуществляют удаление или отделение первого, второго или третьего выходящих потоков.2. Способ по п.1, в котором первый, второй, третий и четвертый реакторы действуют под давление около 50-100 атмосфер.3. Способ по п.1, в котором топливо содержит по существу C-Cуглеводороды, толуол и ксилол.4. Способ по п.1, в котором тяжелый бензин содержит ароматические соединения ≥C.5. Способ по п.1, в котором температура в первом реакторе составляет около 190-300°C.6. Способ по п.1, в котором в котором температура во втором реакторе составляет около 300-450°C.7. Способ по п.1, в котором в котором температура в третьем реакторе составляет около 300-500°C.8. Способ по п.1, в котором в котором температура в четвертом реакторе составляет окол
Claims (32)
1. Способ получения топлива из синтез-газа, включающий стадии:
а) пропускания синтез-газа через первый реактор с целью конверсии синтез-газа в метанол и воду с образованием первого выходящего потока,
б) пропускания первого выходящего потока через второй реактор с целью конверсии метанола в простой диметиловый эфир с образованием второго выходящего потока,
в) пропускания второго выходящего потока через третий реактор с целью конверсии метанола и простого диметилового эфира в топливо и тяжелый бензин с образованием третьего выходящего потока,
г) пропускания третьего выходящего потока через четвертый реактор с целью конверсии тяжелого бензина в изопарафины, нафтены и ароматические соединения с низкой степенью замещения с образованием четвертого выходящего потока, и
д) возвращения непрореагировавшего синтез-газа, содержащегося в четвертом выходящем потоке, в повторный цикл в первый реактор,
причем на протяжении способа не осуществляют удаление или отделение первого, второго или третьего выходящих потоков.
2. Способ по п.1, в котором первый, второй, третий и четвертый реакторы действуют под давление около 50-100 атмосфер.
3. Способ по п.1, в котором топливо содержит по существу C4-C8 углеводороды, толуол и ксилол.
4. Способ по п.1, в котором тяжелый бензин содержит ароматические соединения ≥C8.
5. Способ по п.1, в котором температура в первом реакторе составляет около 190-300°C.
6. Способ по п.1, в котором в котором температура во втором реакторе составляет около 300-450°C.
7. Способ по п.1, в котором в котором температура в третьем реакторе составляет около 300-500°C.
8. Способ по п.1, в котором в котором температура в четвертом реакторе составляет около 100-220°C.
9. Способ по п.1, в котором первый реактор содержит катализаторы CuO/ZnO/Al2O3.
10. Способ по п.1, в котором второй реактор содержит катализаторы на основе гамма-оксида алюминия.
11. Способ по п.1, в котором третий реактор содержит катализаторы ZSM-5.
12. Способ по п.1, в котором четвертый реактор содержит катализатор на основе оксида металла Группы IX или X на алюминийоксидном носителе, восстановленный в присутствии водорода и окиси углерода и в отсутствие серы.
13. Способ по п.12, в котором оксидом металла Группы IX или X является оксид никеля.
14. Способ по п.1, в котором четвертый реактор содержит катализатор на основе оксида металла Группы IX или X в сочетании с катализатором на основе оксида металла Группы VI на алюминийоксидном носителе, восстановленный в присутствии водорода и окиси углерода и в отсутствие серы.
15. Способ по п.14, в котором оксидом металла Группы IX или X является оксид кобальта, а оксидом металла Группы VI является оксид молибдена, образующий молибдат кобальта.
16. Способ по п.1, в котором до осуществления стадии д) четвертый выходящий поток разделяют на первый поток, содержащий воду, второй поток, содержащий непрореагировавший синтез-газ, и третий поток, содержащий топливо.
17. Способ по п.1, в котором нагревают или охлаждают первый, второй и третий выходящие потоки до их подачи во второй, третий и четвертый реакторы, соответственно.
18. Способ по п.1, в котором тяжелый бензин содержит триметилбензол, тетраметилбензол и дурол.
19. Способ по п.1, в котором менее замещенными ароматическими соединениями являются толуол и ксилол.
20. Способ по п.1, в котором температура замерзания третьего выходящего потока составляет от около 30 до около 50°C.
21. Способ по п.1, в котором температура замерзания топлива составляет менее около -5°C.
22. Способ по п.1, в котором выход составляет более около 25% по весу синтез-газа.
23. Способ по п.1, в котором синтез-газ изначально подают непосредственно в третий реактор.
24. Способ по п.23, в котором синтез-газ содержит молекулы алифатических углеводородов и/или олефинов с двумя или более атомами углерода и/или более крупные молекулы циклических и ароматических соединений
25. Система получения готового топлива, содержащая:
а) первый реактор, содержащий первый катализатор для конверсии синтез-газа в метанол и воду,
б) второй реактор, содержащий второй катализатор для конверсии метанола в простой диметиловый эфир,
в) третий реактор, содержащий третий катализатор для конверсии метанола и простого диметилового эфира в топливо и тяжелый бензин,
г) четвертый реактор, содержащий четвертый катализатор для конверсии тяжелого бензина в изопарафины, нафтены и ароматические соединения с низкой степенью замещения,
д) сепаратор для разделения продукта, выходящего из четвертого реактора, на первый поток, содержащий готовое топливо, второй поток, содержащий воду, и третий поток, содержащий непрореагировавший синтез-газ, и
е) поток, возвращаемый в повторный цикл, с целью возврата части третьего потока в повторный цикл в первый реактор.
26. Система по п.25, в которой первым катализатором является CuO/ZnO/Al2O3.
27. Система по п.25, в которой вторым катализатором является гамма-оксид алюминия.
28. Система по п.25, в которой третьим катализатором является ZSM-5.
29. Система по п.25, в которой четвертым катализатором является катализатор на основе оксида металла Группы IX или X на алюминийоксидном носителе, восстановленный в присутствии водорода и окиси углерода и в отсутствие серы.
30. Система по п.29, в которой оксидом металла Группы IX или X является оксид никеля.
31. Система по п.25, в которой четвертый реактор содержит катализатор на основе оксида металла Группы IX или X в сочетании с катализатором на основе оксида металла Группы VI на алюминийоксидном носителе, восстановленный в присутствии водорода и окиси углерода и в отсутствие серы.
32. Система по п.31, в которой оксидом металла Группы IX или X является оксид кобальта, а оксидом металла Группы VI является оксид молибдена, образующий молибдат кобальта.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US12/942,680 | 2010-11-09 | ||
| US12/942,680 US8686206B2 (en) | 2010-11-09 | 2010-11-09 | Single loop multistage fuel production |
| PCT/US2011/059975 WO2012064844A2 (en) | 2010-11-09 | 2011-11-09 | Single loop multistage fuel production |
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| Publication Number | Publication Date |
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| RU2013124424A true RU2013124424A (ru) | 2014-12-20 |
| RU2574390C2 RU2574390C2 (ru) | 2016-02-10 |
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| NZ609789A (en) | 2014-12-24 |
| KR20140064703A (ko) | 2014-05-28 |
| AU2011326572B2 (en) | 2016-02-25 |
| AP2013006910A0 (en) | 2013-06-30 |
| CA2816141A1 (en) | 2012-05-18 |
| US9169166B2 (en) | 2015-10-27 |
| AU2011326572A1 (en) | 2013-05-23 |
| CO6781471A2 (es) | 2013-10-31 |
| KR101899124B1 (ko) | 2018-09-17 |
| IL225986B (en) | 2019-07-31 |
| WO2012064844A2 (en) | 2012-05-18 |
| ZA201303045B (en) | 2014-07-30 |
| CA2816141C (en) | 2018-12-11 |
| US20140199213A1 (en) | 2014-07-17 |
| US20120116137A1 (en) | 2012-05-10 |
| BR112013011571A2 (pt) | 2016-08-09 |
| CN103270139A (zh) | 2013-08-28 |
| US8686206B2 (en) | 2014-04-01 |
| EP2638128A4 (en) | 2016-08-24 |
| WO2012064844A3 (en) | 2012-08-16 |
| EP2638128A2 (en) | 2013-09-18 |
| IL225986A0 (en) | 2013-06-27 |
| CN103270139B (zh) | 2015-11-25 |
| AP3697A (en) | 2016-05-31 |
| MX2013005223A (es) | 2013-09-26 |
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