RU2008139603A - Способ получения продукта синтеза фишера-тропша - Google Patents
Способ получения продукта синтеза фишера-тропша Download PDFInfo
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- 230000015572 biosynthetic process Effects 0.000 title claims abstract 13
- 238000003786 synthesis reaction Methods 0.000 title claims abstract 12
- 238000004519 manufacturing process Methods 0.000 title 1
- 229930195733 hydrocarbon Natural products 0.000 claims abstract 11
- 238000000034 method Methods 0.000 claims abstract 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract 8
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract 8
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract 8
- 239000007789 gas Substances 0.000 claims abstract 7
- 238000002407 reforming Methods 0.000 claims abstract 6
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract 5
- 239000008246 gaseous mixture Substances 0.000 claims abstract 5
- 239000001257 hydrogen Substances 0.000 claims abstract 5
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract 5
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract 4
- 239000001569 carbon dioxide Substances 0.000 claims abstract 4
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract 4
- 238000010438 heat treatment Methods 0.000 claims abstract 4
- 239000000203 mixture Substances 0.000 claims abstract 4
- 230000003647 oxidation Effects 0.000 claims abstract 4
- 238000007254 oxidation reaction Methods 0.000 claims abstract 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract 3
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract 3
- 239000001301 oxygen Substances 0.000 claims abstract 3
- 229910052760 oxygen Inorganic materials 0.000 claims abstract 3
- 125000004432 carbon atom Chemical group C* 0.000 claims abstract 2
- 239000003054 catalyst Substances 0.000 claims abstract 2
- 230000003197 catalytic effect Effects 0.000 claims abstract 2
- 239000011874 heated mixture Substances 0.000 claims abstract 2
- 229910052741 iridium Inorganic materials 0.000 claims abstract 2
- 239000000463 material Substances 0.000 claims abstract 2
- 229910052751 metal Inorganic materials 0.000 claims abstract 2
- 239000002184 metal Substances 0.000 claims abstract 2
- 229910052759 nickel Inorganic materials 0.000 claims abstract 2
- 229910052763 palladium Inorganic materials 0.000 claims abstract 2
- 229910052697 platinum Inorganic materials 0.000 claims abstract 2
- 229910052707 ruthenium Inorganic materials 0.000 claims abstract 2
- 239000000126 substance Substances 0.000 claims abstract 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims 1
- 229910052799 carbon Inorganic materials 0.000 claims 1
- 238000004517 catalytic hydrocracking Methods 0.000 claims 1
- 230000004907 flux Effects 0.000 claims 1
- 239000002994 raw material Substances 0.000 claims 1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/382—Multi-step processes
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
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- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0211—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step
- C01B2203/0216—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step containing a non-catalytic steam reforming step
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
- C01B2203/0255—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a non-catalytic partial oxidation step
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- C01B2203/0415—Purification by absorption in liquids
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- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
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- C01B2203/06—Integration with other chemical processes
- C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
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- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
- C01B2203/0827—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel at least part of the fuel being a recycle stream
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- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
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- C01B2203/14—Details of the flowsheet
- C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
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- C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
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- C01B2203/1614—Controlling the temperature
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- C01B2203/169—Controlling the feed
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- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1022—Fischer-Tropsch products
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Abstract
1. Способ получения продукта синтеза Фишера-Тропша из газообразной смеси углеводородов, содержащей метан, этан и необязательно углеводорода с более высоким числом атомов углерода, путем осуществления следующих стадий: ! (a) адиабатический предварительный риформинг углеводородной смеси в присутствии катализатора риформинга, содержащего оксидный материал носителя и металл, который выбирают из группы, состоящей из Pt, Ni, Ru, Ir, Pd и Co, с целью превращения этана и необязательных углеводородов с более высоким числом атомов углерода в метан, диоксид углерода и водород, ! (b) нагревание газообразной смеси, полученной на стадии (а), до температуры выше, чем 650°C, ! (c) осуществление некаталитического парциального окисления путем введения в контакт нагретой смеси со стадии (b) с источником кислорода в реакторной горелке, с образованием выходящего из реактора потока, имеющего температуру между 1100 и 1500°C, ! (d) осуществление синтеза Фишера-Тропша с использованием в качестве сырья газа, содержащего водород и монооксид углерода, который получен на стадии (с) и ! (e) где продукт синтеза, полученный на стадии (d), разделяют на относительно легкий поток и относительно тяжелый поток, причем относительно тяжелый поток содержит продукт синтеза Фишера-Тропша, а относительно легкий поток содержит непревращенный синтез-газ, инертные вещества, диоксид углерода и C1-С3 углеводороды, и где первую часть легкого потока рециркулируют на стадию (а) для того, чтобы подвергнуть ее предварительному риформингу, и где вторую часть легкого потока рециркулируют в реакторную горелку стадии (с) для того, чтобы подвергнуть ее парциальному окислению, и где темпер�
Claims (10)
1. Способ получения продукта синтеза Фишера-Тропша из газообразной смеси углеводородов, содержащей метан, этан и необязательно углеводорода с более высоким числом атомов углерода, путем осуществления следующих стадий:
(a) адиабатический предварительный риформинг углеводородной смеси в присутствии катализатора риформинга, содержащего оксидный материал носителя и металл, который выбирают из группы, состоящей из Pt, Ni, Ru, Ir, Pd и Co, с целью превращения этана и необязательных углеводородов с более высоким числом атомов углерода в метан, диоксид углерода и водород,
(b) нагревание газообразной смеси, полученной на стадии (а), до температуры выше, чем 650°C,
(c) осуществление некаталитического парциального окисления путем введения в контакт нагретой смеси со стадии (b) с источником кислорода в реакторной горелке, с образованием выходящего из реактора потока, имеющего температуру между 1100 и 1500°C,
(d) осуществление синтеза Фишера-Тропша с использованием в качестве сырья газа, содержащего водород и монооксид углерода, который получен на стадии (с) и
(e) где продукт синтеза, полученный на стадии (d), разделяют на относительно легкий поток и относительно тяжелый поток, причем относительно тяжелый поток содержит продукт синтеза Фишера-Тропша, а относительно легкий поток содержит непревращенный синтез-газ, инертные вещества, диоксид углерода и C1-С3 углеводороды, и где первую часть легкого потока рециркулируют на стадию (а) для того, чтобы подвергнуть ее предварительному риформингу, и где вторую часть легкого потока рециркулируют в реакторную горелку стадии (с) для того, чтобы подвергнуть ее парциальному окислению, и где температуру на стадии (а) регулируют, устанавливая количество легкого потока, которое рециркулируют на стадию (а).
2. Способ по п.1, в котором количество легкого потока, которое рециркулируют на стадию (а), является таким, что температура газа, полученного на стадии (а), находится между 350 и 530°C.
3. Способ по п.1, в котором молярное соотношение пара к углероду (в виде углеводорода и СО) на стадии (а) находится между 0,1 и 1.
4. Способ по п.1, в котором температуру газообразной смеси на стадии (b) повышают до температуры между 750 и 900°C.
5. Способ по п.1, в котором нагревание на стадии (b) осуществляют путем косвенного теплообмена между потоком, выходящим со стадии (с), и газообразной смесью предварительного риформинга, полученной на стадии (а).
6. Способ по п.1, в котором нагревание на стадии (b) осуществляют в факельном нагревателе.
7. Способ по п.1, в котором стадию (с) осуществляют путем введения в контакт нагретой на стадии (b) смеси с кислородсодержащим газом в горелке, расположенной наверху вертикально расположенного реакторного аппарата, с образованием выходящего из реактора потока, имеющего температуру между 1200 и 1400°C и молярное соотношение Н2/СО от 1,6 до 2,2.
8. Способ по п.1, в котором легкий поток содержит между 5 и 30 мол.% монооксида углерода и между 5 и 30 мол.% водорода.
9. Способ по п.1, в котором содержание легкого потока в суммарном сырье на стадии (а) находится между 5 и 50 мол.%.
10. Способ по одному из пп.1-9, в котором относительно тяжелый поток содержит продукт синтеза Фишера-Тропша, полученный на стадии (d), и подвергается стадии гидрокрекинга с образованием газойля в качестве продукта.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NG36/2006 | 2006-03-07 | ||
| NG3606 | 2006-03-07 | ||
| EP06117261 | 2006-07-14 | ||
| EP06117261.5 | 2006-07-14 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| RU2008139603A true RU2008139603A (ru) | 2010-04-20 |
| RU2430140C2 RU2430140C2 (ru) | 2011-09-27 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| RU2008139603/04A RU2430140C2 (ru) | 2006-03-07 | 2007-03-05 | Способ получения продукта синтеза фишера-тропша |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US7795317B2 (ru) |
| EP (1) | EP1991639B1 (ru) |
| AU (1) | AU2007222475B2 (ru) |
| MY (1) | MY147506A (ru) |
| RU (1) | RU2430140C2 (ru) |
| WO (1) | WO2007101831A1 (ru) |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FI119522B (fi) * | 2007-08-13 | 2008-12-15 | Waertsilae Finland Oy | Aluksen koneistosovitelma |
| US9115324B2 (en) | 2011-02-10 | 2015-08-25 | Expander Energy Inc. | Enhancement of Fischer-Tropsch process for hydrocarbon fuel formulation |
| US9156691B2 (en) | 2011-04-20 | 2015-10-13 | Expander Energy Inc. | Process for co-producing commercially valuable products from byproducts of heavy oil and bitumen upgrading process |
| US9169443B2 (en) | 2011-04-20 | 2015-10-27 | Expander Energy Inc. | Process for heavy oil and bitumen upgrading |
| US8889746B2 (en) | 2011-09-08 | 2014-11-18 | Expander Energy Inc. | Enhancement of Fischer-Tropsch process for hydrocarbon fuel formulation in a GTL environment |
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- 2007-03-05 MY MYPI20082547A patent/MY147506A/en unknown
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- 2007-03-05 EP EP20070726627 patent/EP1991639B1/en not_active Not-in-force
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| RU2430140C2 (ru) | 2011-09-27 |
| MY147506A (en) | 2012-12-14 |
| AU2007222475A1 (en) | 2007-09-13 |
| US20070213414A1 (en) | 2007-09-13 |
| EP1991639B1 (en) | 2015-04-22 |
| EP1991639A1 (en) | 2008-11-19 |
| US7795317B2 (en) | 2010-09-14 |
| WO2007101831A1 (en) | 2007-09-13 |
| AU2007222475B2 (en) | 2010-07-08 |
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