CN101015784B - 用于进行烃原料的蒸汽重整反应的方法 - Google Patents
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- 238000000034 method Methods 0.000 title claims abstract description 12
- 238000006555 catalytic reaction Methods 0.000 title 1
- 238000006243 chemical reaction Methods 0.000 claims abstract description 48
- 239000003054 catalyst Substances 0.000 claims abstract description 30
- 239000004215 Carbon black (E152) Substances 0.000 claims description 16
- 229930195733 hydrocarbon Natural products 0.000 claims description 16
- 150000002430 hydrocarbons Chemical class 0.000 claims description 16
- 239000000203 mixture Substances 0.000 claims description 5
- 238000000629 steam reforming Methods 0.000 claims description 5
- 239000000376 reactant Substances 0.000 abstract description 12
- 239000007789 gas Substances 0.000 description 19
- 230000009977 dual effect Effects 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000010410 dusting Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
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Abstract
用于非绝热式反应的方法,包括:将第一反应剂流引入第一反应区以及将第二反应剂流引入第二反应区;按照与换热介质间接换热的方式使第一反应剂在第一反应区与催化剂接触,使第二反应剂在第二反应区与催化剂接触,并各自排出经蒸汽重整的产物气体;按照与换热介质呈间接换热关系的方式将第一反应区的催化剂布置到管式反应器内,将第二反应区的催化剂式布置在换热区的管际空间。
Description
本申请是基于申请日为2000年12月2日、申请号为00137042.1的申请所提交的分案申请。
技术领域
本发明涉及一种用于进行非绝热式反应的方法和反应器系统,所述反应在催化剂的存在下,按照与合适的换热介质间接换热的方式放热或吸热地发生在工艺气体中。
发明内容
因此,本发明的总目的是提供一种用于进行非绝热式反应的方法,该方法包括以下步骤:
并列地将第一反应剂物流引入第一反应区以及将第二反应剂物流引入第二反应区,
在反应条件下,使第一反应剂物流按照与换热介质间接换热的方式在第一反应区与催化剂接触,并且使第二反应剂流按照与换热介质间接换热的方式在第二反应区与催化剂接触,将第一反应区的催化剂按照与换热介质呈间接换热关系的方式布置在管式反应器内,方法是将所述介质引入同心地环绕着具有第一反应区的管式反应器的管状换热区内,将第二反应区的催化剂按照与换热介质呈间接换热关系的方式布置在换热区的管际空间。
具体地说,本发明涉及一种用于进行烃原料的蒸汽重整反应的方法,该方法包括以下步骤:
提供烃原料的第一部分、第二部分和第三部分;
并列地将烃原料的第一部分引入第一反应区、将烃原料的第二部分引入第二反应区以及将第三部分引入自热反应器;
在反应条件下,并列地使第一物流按照与加热气体间接换热的方式在第一反应区与催化剂接触,并且使第二物流按照与加热气体间接换热的方式在第二反应区与催化剂接触;
其中将第一反应区的催化剂按照与加热气体呈间接换热关系的方式布置到管式反应器内,将所述加热气体引入同心地环绕着具有第一反应区的管式反应器的管状换热区内,将第二反应区的催化剂按照与加热气体呈间接换热关系的方式布置在换热区的管际空间,并且所述加热气体是束自自热反应器的流出物流和经蒸汽重整的产物气体的混合物,其中所述经蒸汽重整的产物气体从所述第一和第二反应区中的催化剂中排出。
本发明尤其可用于进行烃原料的汽蒸重整反应,该反应所用的热量由自热蒸汽重整反应器的热流出气和蒸汽重整产物气体提供。
附图说明
在以下的说明中,参照附图更详细地阐述了本发明反应系统的一个具体实施方案,其中图1示意性地展示了用于由烃原料的蒸汽重整来生产一种具有高含量的氢气和/或一氧化碳的气体的反应系统。
具体实施方式
蒸汽重整是一种吸热的化学反应,该反应中烃与蒸汽在蒸汽重整催化剂上反应,条件是向发生反应的位置提供适当的热量。
该实施方案中采用的反应器系统由三个反应器构成,其中蒸汽重整反应在这三个反应器中完成。三个反应器R1、R2和R3并联运作。
R1是绝热式反应器。供R1中的反应使用的反应剂由烃、蒸汽和富氧气体组成,该反应剂在合适的温度下被引入反应器中并混合。氧气和烃以燃烧的方式反应并产生由剩余的烃、蒸汽和燃烧所得产物组成的热气。随后,使该热气通过重整催化剂床并催化转化成由氢气、一氧化碳和二氧化碳组成的热混合物。
R2和R3是两个活塞流反应器。供R2和R3中的反应使用的反应剂是烃与蒸汽的混合物,该混合物在流过重整催化剂床之前被加热到合适的温度。R2和R3的催化剂床被器壁环绕并封闭。热气在该器壁外部与催化剂床内的反应气体呈逆向流动。热量通过该器壁由热气传递给反应气体,同时该反应气体被转化成为由氢气、一氧化碳和二氧化碳组成的热混合物。
将出自R1、R2和R3的产物气体混合并形成在R2和R3的器壁外部流动的热气,在此,它们成为R2和R3内反应的热源。该热气被称为加热气体。
作为本发明的一个一般性优点,R2和R3的器壁可以被安排成能给加热气体形成最佳通道的布置。
本发明还提供了一种特别适用于进行以上反应的反应系统。一般,本发明的反应系统包括以并联方式连接的适于安放催化剂和接纳反应剂流的第一和第二反应室,第一室呈反应管的形式,其中
第一换热区同心且有间隔地环绕着第一反应室,而第二反应室环绕着第二换热区。
反应器R2包含安放在管内的催化剂。反应器R3将催化剂安放在管外。组合的反应器R2和R3包含一些双重管,其中的内管填装有催化剂(R2),该双重管另外还被布置成使双重管之间的空间也填装有催化剂的形式,即反应器R3。来自由反应器R1、R2和R3产生的混合产物气体的显热被循环回反应器R2和R3。产物气体按照与反应器R2和R3中的流动呈逆流的方式在双重管形成的环形通道中流动。热量通过双重管的内壁供给反应器R2,而反应器R3由双重管的外壁供热。
如图2所示的组合反应器的优点是以最佳的方式使用了换热通道,即内壁和外壁均被用作换热表面,因此使昂贵的材料得到了最佳利用。与其它类型的热交换重整器相比,这还使设备的设计非常紧凑,同时达到了低的压降。
在冷却产物气体时,存在一定程度的金属尘腐蚀的危险。组合反应器设计的另一个优点就是将这种金属尘的危险限制在有限的表面。
双重管的尺寸一般为:内管的外径(OD)为50-140mm,外管的外径为80-170mm。该管的布置可以(但不是必须)按以下方式进行:使内管的热交换/面积/催化剂体积的比值与外管的该比值相等。
Claims (1)
1.一种用于进行烃原料的蒸汽重整反应的方法,该方法包括以下步骤:
提供烃原料的第一部分、第二部分和第三部分;
并列地将烃原料的第一部分引入第一反应区、将烃原料的第二部分引入第二反应区以及将第三部分引入自热反应器;
在反应条件下,并列地使第一物流按照与加热气体间接换热的方式在第一反应区与催化剂接触,并且使第二物流按照与加热气体间接换热的方式在第二反应区与催化剂接触;
其中将第一反应区的催化剂按照与加热气体呈间接换热关系的方式布置到管式反应器内,将所述加热气体引入同心地环绕着具有第一反应区的管式反应器的管状换热区内,将第二反应区的催化剂按照与加热气体呈间接换热关系的方式布置在换热区的管际空间,并且所述加热气体是来自自热反应器的流出物流和经蒸汽重整的产物气体的混合物,其中所述经蒸汽重整的产物气体从所述第一和第二反应区中的催化剂中排出。
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CN101015784B true CN101015784B (zh) | 2010-06-16 |
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CN2006100899056A Expired - Lifetime CN101015784B (zh) | 1999-12-02 | 2000-12-02 | 用于进行烃原料的蒸汽重整反应的方法 |
CN00137042A Pending CN1314203A (zh) | 1999-12-02 | 2000-12-02 | 用于进行非绝热式催化反应的方法和反应器 |
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US (1) | US6726851B1 (zh) |
EP (1) | EP1106570B1 (zh) |
JP (1) | JP5190162B2 (zh) |
CN (2) | CN101015784B (zh) |
CA (1) | CA2326950C (zh) |
ES (1) | ES2427927T3 (zh) |
NO (1) | NO324482B1 (zh) |
PT (1) | PT1106570E (zh) |
RU (1) | RU2261756C2 (zh) |
Families Citing this family (15)
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EP1413547A1 (en) * | 2002-09-26 | 2004-04-28 | Haldor Topsoe A/S | Process for the production of synthesis gas |
DE60336444D1 (de) * | 2002-09-26 | 2011-05-05 | Haldor Topsoe As | Verfahren zur Herstellung von Synthesegas |
EP1750836A4 (en) * | 2004-05-28 | 2008-04-02 | Hyradix Inc | METHOD FOR PRODUCING HYDROGEN BY PARTIAL OXIDATION / STEAM REFORMING |
CN100408156C (zh) * | 2006-09-18 | 2008-08-06 | 西安交通大学 | 一种金属泡沫催化重整反应器 |
US8261700B2 (en) * | 2008-06-26 | 2012-09-11 | Haldor Topsoe A/S | Steam superheater |
EP2421794B1 (en) | 2009-04-22 | 2014-09-03 | Shell Internationale Research Maatschappij B.V. | Process for the preparation of hydrogen and carbon monoxide containing gas |
US8759406B2 (en) | 2009-04-22 | 2014-06-24 | Shell Oil Company | Production of a synthesis gas blend and use in a fischer-tropsch process |
PL2526044T3 (pl) | 2010-01-19 | 2019-05-31 | Topsoe Haldor As | Sposób reformowania węglowodorów |
EP2450420A1 (en) | 2010-11-08 | 2012-05-09 | Shell Internationale Research Maatschappij B.V. | Multi stage process for producing hydrocarbons from syngas |
WO2013004254A1 (en) | 2011-07-01 | 2013-01-10 | Haldor Topsøe A/S | Heat exchange reactor |
US9029429B2 (en) | 2011-12-13 | 2015-05-12 | Shell Oil Company | Fischer-tropsch process |
EP2676924A1 (en) * | 2012-06-21 | 2013-12-25 | Haldor Topsoe A/S | Process for Reforming Hydrocarbons |
RU2588617C1 (ru) * | 2015-03-11 | 2016-07-10 | Федеральное государственное бюджетное образовательное учреждение высшего образования "Казанский национальный исследовательский технический университет им. А.Н. Туполева-КАИ" (КНИТУ-КАИ) | Способ проведения экзотермических и эндотермических каталитических процессов частичного превращения углеводородов и реакторная группа для его осуществления |
EP3720813B1 (en) | 2017-12-08 | 2023-06-07 | Topsoe A/S | System and process for production of synthesis gas |
CA3200137A1 (en) | 2021-01-28 | 2022-08-04 | Anders Helbo Hansen | Catalytic heat exchange reactor with helical flow |
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- 2000-11-17 ES ES00125077T patent/ES2427927T3/es not_active Expired - Lifetime
- 2000-11-17 EP EP00125077.8A patent/EP1106570B1/en not_active Expired - Lifetime
- 2000-11-17 PT PT125077T patent/PT1106570E/pt unknown
- 2000-11-28 US US09/722,482 patent/US6726851B1/en not_active Expired - Lifetime
- 2000-11-28 CA CA002326950A patent/CA2326950C/en not_active Expired - Lifetime
- 2000-11-30 JP JP2000365084A patent/JP5190162B2/ja not_active Expired - Fee Related
- 2000-12-01 RU RU2000130045/12A patent/RU2261756C2/ru not_active IP Right Cessation
- 2000-12-01 NO NO20006105A patent/NO324482B1/no not_active IP Right Cessation
- 2000-12-02 CN CN2006100899056A patent/CN101015784B/zh not_active Expired - Lifetime
- 2000-12-02 CN CN00137042A patent/CN1314203A/zh active Pending
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US4909808A (en) * | 1987-10-14 | 1990-03-20 | The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration | Steam reformer with catalytic combustor |
Also Published As
Publication number | Publication date |
---|---|
CN101015784A (zh) | 2007-08-15 |
CN1314203A (zh) | 2001-09-26 |
CA2326950A1 (en) | 2001-06-02 |
US6726851B1 (en) | 2004-04-27 |
NO324482B1 (no) | 2007-10-29 |
JP5190162B2 (ja) | 2013-04-24 |
CA2326950C (en) | 2008-07-29 |
RU2261756C2 (ru) | 2005-10-10 |
EP1106570B1 (en) | 2013-08-28 |
ES2427927T3 (es) | 2013-11-04 |
NO20006105D0 (no) | 2000-12-01 |
NO20006105L (no) | 2001-06-05 |
PT1106570E (pt) | 2013-10-15 |
EP1106570A2 (en) | 2001-06-13 |
EP1106570A3 (en) | 2003-04-02 |
JP2001190946A (ja) | 2001-07-17 |
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