EP1651563A1 - Apparat zur erzeugung von wasserstoff - Google Patents
Apparat zur erzeugung von wasserstoffInfo
- Publication number
- EP1651563A1 EP1651563A1 EP04802817A EP04802817A EP1651563A1 EP 1651563 A1 EP1651563 A1 EP 1651563A1 EP 04802817 A EP04802817 A EP 04802817A EP 04802817 A EP04802817 A EP 04802817A EP 1651563 A1 EP1651563 A1 EP 1651563A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- stage
- cooling
- methanation
- generating hydrogen
- hydrogen according
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 239000001257 hydrogen Substances 0.000 title claims abstract description 29
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 29
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 28
- 238000001816 cooling Methods 0.000 claims abstract description 54
- 239000002826 coolant Substances 0.000 claims abstract description 21
- 239000007789 gas Substances 0.000 claims abstract description 18
- 239000003054 catalyst Substances 0.000 claims abstract description 15
- 238000006243 chemical reaction Methods 0.000 claims abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 5
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 5
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 5
- 230000000694 effects Effects 0.000 claims abstract description 4
- 230000003197 catalytic effect Effects 0.000 claims abstract description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 25
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 25
- 230000002211 methanization Effects 0.000 claims description 17
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 14
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 7
- 239000001569 carbon dioxide Substances 0.000 claims description 6
- 238000000034 method Methods 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 2
- 238000002407 reforming Methods 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims 1
- 150000002431 hydrogen Chemical class 0.000 claims 1
- 239000000446 fuel Substances 0.000 description 8
- 238000013461 design Methods 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 238000012546 transfer Methods 0.000 description 3
- 230000001419 dependent effect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 230000009931 harmful effect Effects 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 238000000629 steam reforming Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
- B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- 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
- C01B3/38—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
- C01B3/384—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 the catalyst being continuously externally heated
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- 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
- C01B3/48—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 followed by reaction of water vapour with carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- 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
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
- C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
- C01B3/586—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction the reaction being a methanation reaction
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
-
- C—CHEMISTRY; METALLURGY
- 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
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- 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
- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
-
- C—CHEMISTRY; METALLURGY
- 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
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0435—Catalytic purification
- C01B2203/0445—Selective methanation
-
- C—CHEMISTRY; METALLURGY
- 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
- C01B2203/04—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
- C01B2203/047—Composition of the impurity the impurity being carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- 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
- C01B2203/08—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
- C01B2203/0816—Heating by flames
-
- C—CHEMISTRY; METALLURGY
- 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
- C01B2203/08—Methods of heating or cooling
- C01B2203/0872—Methods of cooling
Definitions
- the invention relates to an apparatus for generating hydrogen according to the preamble of patent claim 1.
- the catalyst stage is followed by a so-called methanation stage, which (by means of hydrogen) converts the remaining carbon monoxide into methane gas.
- the entry temperature of the reformate gas containing carbon monoxide into the methanation stage is generally about 240 ° C. Since the methanization process is exothermic, cooling of the methanization stage is required.
- a flow guide housing for a cooling medium is provided which, depending on the design of the methanization stage, is assigned to the stage either from the outside or from the inside (for example in the case of a hollow-cylindrical design). The flow medium can flow through the cooling medium in cocurrent or countercurrent to the reformate stream as required.
- the object of the invention is accordingly to ensure, in an apparatus of the type mentioned at the outset, in the simplest possible manner that this retroshift reaction does not take place and the carbon monoxide content in the reformate gas at the exit of the methanation stage is as low as possible, preferably significantly less than 100 ppm is.
- the flow guide housing arranged in the axial direction one behind the other has at least two, preferably three or more cooling zones with different cooling effects.
- the use of at least two cooling zones leads - depending on the design of the cooling zones - to a step-like or continuously changing temperature profile within the methanation stage, which, if the cooling medium temperature is appropriate, in turn means that despite the exothermic methanation process, the temperature towards the exit of the methanation stage decreases significantly and accordingly the undesired retroshift reaction does not occur.
- the particular advantage of the invention is therefore that the temperature profile within the methanation stage can be influenced in a targeted manner and in this way a minimal carbon monoxide content in the reformate gas can be achieved.
- k may even be dispensed to a so ⁇ called "Air Bleed", so far the Me ⁇ than Deutschenscut downstream and the fuel cell was connected upstream and oxidized in which by means of small amounts of oxygen, the rest ⁇ Liche in the reformate containing carbon monoxide has been.
- Figure 1 shows schematically in section the apparatus according to the invention with a methanization stage with four cooling zones;
- FIG. 2 shows a diagram of the temperature profile plotted over the barrel length x within the methanization stage when using a cooling zone (prior art);
- FIG. 3 shows a diagram of the temperature profile plotted over the barrel length x within the methanization stage when using four cooling zones
- FIG. 4 shows a diagram of the temperature profile plotted over the barrel length x within the four cooling zones
- FIG. 5 shows schematically, in section, two further embodiments of the flow guide housing at the methanization stage (summarized in one illustration for the sake of simplicity);
- Figure 6 shows schematically in section a further embodiment of the flow guide housing at the methanization stage.
- the reformer stage 1 having a reforming catalyst is preferably, as shown, designed as a steam reforming stage which is heated with a burner 9, in particular a gas burner, that is to say in this stage, for example, CH 4 and H 2 O in CO, CO2 and H2 implemented (endothermic reaction).
- the reformer stage 1 is preferably designed as a hollow cylinder, as shown.
- the apparatus according to the invention further comprises at least one catalyst stage 2 downstream of the reformer stage 1 for the catalytic conversion of the carbon monoxide, ie. H. In any case, this is partially converted into carbon dioxide, which is harmless to the fuel cell.
- the catalyst stage 2 it is also advantageously provided in the catalyst stage 2 that it is of hollow cylindrical design. This requirement leads to a more uniform temperature profile and thus to better carbon monoxide conversion within catalyst stage 2.
- the apparatus comprises an axially flowing methane downstream of the catalyst stage 2 s iststress 3, which serves, as mentioned, to methanize as much of the remaining carbon monoxide contained in the reformate gas by means of hydrogen.
- a flow guide housing 4 which extends in the axial flow direction, for a cooling medium.
- the methanization stage 3 is also preferably of hollow cylindrical design.
- the reformer stage 1, the catalyst stage 2 and the methanation stage 3 are arranged one behind the other in the axial flow direction.
- the steps are arranged one behind the other defining a continuous annular space in the axial flow direction.
- the flow guide housing 4 arranged in the axial direction one behind the other has at least two, preferably three and more cooling zones 5, 6, 7, 8 with different cooling effects.
- the flow guide housing 4 is divided into four cooling zones 5, 6, 7, 8, to each of which the cooling medium can be fed separately.
- two zones are already suitable for solving the task defined at the beginning. The more cooling zones are provided, the more precisely the temperature profile can be determined within the methanation stage, but the greater the expenditure on equipment. Four zones have proven to be a good choice here.
- cooling zones 5, 6, 7, 8 are optionally arranged on the inside and / or outside of the methanization stage 3 (see FIG. 6).
- the cooling zones 5, 6, 7, 8 preferably enclose them axially Annular spaces arranged one behind the other, the methanation stage 3 or are enclosed by the methanation stage 3 in the case of a hollow cylindrical configuration (again, see FIG. 6).
- each cooling zone 5, 6, 7, 8 each has at least one coolant supply and one coolant discharge connection 11, each cooling zone 5, 6, 7, 8 also advantageously being dependent on the cooling medium Co-flow (not shown) or countercurrent to methanation stage 3 can be flowed through.
- the cooling zones 5, 6, 7, 8 are supplied with different cooling media.
- cooling medium used is supplied to the individual zones 5, 6, 7, 8 at different temperatures, or that when different cooling media are used, these are themselves at different temperatures, for example through the use of heat exchangers (not shown).
- Ficjur 2 shows a temperature profile over the barrel length x (see FIG. 1) within a methanation stage which has only one cooling zone (prior art).
- the methanation step converts carbon monoxide and hydrogen back into hydrocarbon gas (methane) in order to reduce the carbon monoxide content in the reformate gas.
- methanation is an exothermic process
- the temperature in the stage initially rises and then falls to a value just below the inlet temperature due to the cooling.
- the carbon monoxide content is usually about 120 ppm, that is too much to direct the reformate gas directly to the fuel cell.
- the methanation stage is therefore usually followed by an "air bleed" in order to also remove this proportion of carbon monoxide.
- FIG. 3 shows a corresponding temperature profile that can be set when using the cooling zone division according to the invention.
- the temperature in the methanation stage in this solution thus drops continuously from 240 ° C to about 220 ° C, with the result that, especially at the end of the methanization stage, no retroshift reaction can take place, since the temperatures in this cooling zone are too low are.
- the reference numerals 5, 6, 7, 8 and the dotted lines in FIG. 3 are intended to clarify the arrangement area of the cooling zones.
- FIG. 4 shows the temperature profile within the individual cooling zones. It is particularly noticeable that a kind of sawtooth profile arises due to the cooling in counterflow, but the temperature peaks continue to drop towards the exit of the stage, which inevitably leads to the desired, falling temperature profile within the methanization stage.
- the cooling zones 5, 6, 7, 8 arranged one behind the other in the axial direction are directly hydraulically connected to one another, but have different flow cross-sections.
- a direct hydraulic separation of the cooling zones 5, 6, 7, 8 is therefore not mandatory, but can also be achieved by a suitable choice of the axial flow cross sections the heat transfer in the individual areas of the methanation stage can be influenced in a targeted manner.
- the cooling zones 5, 6, 7, 8 have flow cross sections that are stepped in the axial direction.
- continuously changing flow cross-sections are also provided, in both cases the cooling zones 5, 6, 7, 8 can be flowed through by the cooling medium either in cocurrent or countercurrent to the methanation stage 3.
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10356650A DE10356650A1 (de) | 2003-12-02 | 2003-12-02 | Apparat zur Erzeugung von Wasserstoff |
PCT/DE2004/002608 WO2005054125A1 (de) | 2003-12-02 | 2004-11-25 | Apparat zur erzeugung von wasserstoff |
Publications (1)
Publication Number | Publication Date |
---|---|
EP1651563A1 true EP1651563A1 (de) | 2006-05-03 |
Family
ID=34638328
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP04802817A Withdrawn EP1651563A1 (de) | 2003-12-02 | 2004-11-25 | Apparat zur erzeugung von wasserstoff |
Country Status (5)
Country | Link |
---|---|
US (1) | US20080019884A1 (de) |
EP (1) | EP1651563A1 (de) |
JP (1) | JP2007513044A (de) |
DE (1) | DE10356650A1 (de) |
WO (1) | WO2005054125A1 (de) |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP5037878B2 (ja) * | 2006-08-25 | 2012-10-03 | 日本碍子株式会社 | 選択透過膜型反応器及び水素ガスの製造方法 |
EP2602228B1 (de) * | 2010-08-03 | 2017-11-08 | Panasonic Intellectual Property Management Co., Ltd. | Vorrichtung zur wasserstoffproduktion und brennstoffzellensystem |
EP3045425B1 (de) * | 2013-09-09 | 2019-11-06 | Chiyoda Corporation | Vorrichtung und verfahren zur herstellung von wasserstoff und synthetischem erdgas |
JP6194143B2 (ja) * | 2013-09-09 | 2017-09-06 | 千代田化工建設株式会社 | 水素及び合成天然ガスの製造装置及び製造方法 |
Family Cites Families (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3441393A (en) * | 1966-01-19 | 1969-04-29 | Pullman Inc | Process for the production of hydrogen-rich gas |
DE10213326A1 (de) * | 2002-03-25 | 2003-10-16 | Viessmann Werke Kg | Apparat zur Erzeugung von Wasserstoff |
GB9713474D0 (en) * | 1997-06-27 | 1997-09-03 | Johnson Matthey Plc | Catalytic reactor |
GB9720353D0 (en) * | 1997-09-25 | 1997-11-26 | Johnson Matthey Plc | Hydrogen purification |
JP3723680B2 (ja) * | 1998-03-05 | 2005-12-07 | 三洋電機株式会社 | Co除去装置およびco除去装置の運転方法 |
JP2000185901A (ja) * | 1998-12-21 | 2000-07-04 | Aisin Seiki Co Ltd | 改質装置および燃料電池システム |
JP2000256003A (ja) * | 1999-03-08 | 2000-09-19 | Osaka Gas Co Ltd | 水素リッチガス中のco除去方法 |
JP3772619B2 (ja) * | 1999-12-28 | 2006-05-10 | 松下電器産業株式会社 | 水素発生装置 |
US6797420B2 (en) * | 1999-12-28 | 2004-09-28 | Matsushita Electric Industrial Co., Ltd. | Power generation device and operation method therefor |
DE10057537A1 (de) * | 2000-11-20 | 2002-06-06 | Viessmann Werke Kg | Apparat zur Erzeugung von Wasserstoff |
AU2002230936B2 (en) * | 2000-12-13 | 2007-03-22 | Texaco Development Corporation | Single chamber compact fuel processor |
JP2002282690A (ja) * | 2001-03-26 | 2002-10-02 | Osaka Gas Co Ltd | 一酸化炭素除去用触媒および一酸化炭素除去方法ならびに一酸化炭素除去反応器 |
JP3853632B2 (ja) * | 2001-10-26 | 2006-12-06 | 三菱電機株式会社 | 燃料電池発電装置用一酸化炭素除去器及び運転方法 |
CA2478797C (en) * | 2002-03-15 | 2010-05-04 | Matsushita Electric Works, Ltd. | Reforming apparatus and operation method thereof |
WO2003080505A1 (de) * | 2002-03-25 | 2003-10-02 | Viessmann Werke Gmbh & Co. Kg | Vorrichtung zur erzeugung von wasserstoff |
JP2003277013A (ja) * | 2002-03-27 | 2003-10-02 | Osaka Gas Co Ltd | 一酸化炭素除去方法及び固体高分子型燃料電池システム |
DE10250793A1 (de) * | 2002-10-30 | 2004-05-19 | Viessmann Werke Gmbh & Co Kg | Apparat zur Erzeugung von Wasserstoff und Verfahren zum Betrieb eines solchen Apparats |
-
2003
- 2003-12-02 DE DE10356650A patent/DE10356650A1/de not_active Ceased
-
2004
- 2004-11-25 EP EP04802817A patent/EP1651563A1/de not_active Withdrawn
- 2004-11-25 US US10/581,582 patent/US20080019884A1/en not_active Abandoned
- 2004-11-25 WO PCT/DE2004/002608 patent/WO2005054125A1/de active Application Filing
- 2004-11-25 JP JP2006541796A patent/JP2007513044A/ja active Pending
Non-Patent Citations (1)
Title |
---|
See references of WO2005054125A1 * |
Also Published As
Publication number | Publication date |
---|---|
DE10356650A8 (de) | 2005-12-01 |
DE10356650A1 (de) | 2005-07-07 |
JP2007513044A (ja) | 2007-05-24 |
WO2005054125A1 (de) | 2005-06-16 |
US20080019884A1 (en) | 2008-01-24 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
DE60025124T2 (de) | Methode und Vorrichtung zur Wasserstoffherstellung mittels Reformierung | |
DE102009059310A1 (de) | Hocheffizientes Verfahren zur katalytischen Methanisierung von Kohlendioxid und Wasserstoff enthaltenden Gasgemischen | |
EP1571123A1 (de) | Reformer und Verfahren zum Umsetzen von Brennstoff und Oxidationsmittel zu Reformat | |
EP0814054B1 (de) | Reformierungsreaktor, insbesondere zur Wasserdampfreformierung von Methanol | |
DE4221837C1 (en) | Shrouded catalytic reformer tube - with partially enclosed gas mixing zone, for prodn. of synthesis gas | |
EP2758338B1 (de) | Verfahren zur herstellung von synthesegas | |
EP1427668B9 (de) | Vorrichtung zur erzeugung von wasserstoff | |
WO2005054125A1 (de) | Apparat zur erzeugung von wasserstoff | |
EP3577066B1 (de) | Verfahren zur behandlung eines synthesegasstroms | |
DE102018113737A1 (de) | Verfahren und Reaktorsystem zur Durchführung katalytischer Gasphasenreaktionen | |
DE19955892C2 (de) | Vorrichtung zur Reformierung eines Kohlenwasserstoffs mit langkettigen Kohlenwasserstoffanteilen | |
DE19907665A1 (de) | Vorrichtung zur Ausnutzung bei einer katalytischen Reaktion enstehender Wärme | |
DE19958404C2 (de) | Vorrichtung zur selektiven katalytischen Oxidation von Kohlenmonoxid | |
DE102015210803A1 (de) | Festlegung von Druck, Temperatur und S/C-Verhältnis für einen rußfreien ATR-Betrieb | |
DE10213326A1 (de) | Apparat zur Erzeugung von Wasserstoff | |
EP0867962B1 (de) | Zweistufiger Reformierungsreaktor zur Wasserdampfreformierung von Methanol | |
WO2002032807A1 (de) | Verfahren zur gewinnung von wasserstoff aus kohlenwasserstoff | |
EP3860750B1 (de) | Festbettanordnung | |
DE102008017344A1 (de) | Verfahren und Reaktor zur Durchführung exothermer und endothermer Reaktionen | |
EP0326662A1 (de) | Mehrstufiges Verfahren zur Erzeugung von wasserstoff- und kohlenmonoxidhaltigen Synthesegasen | |
WO2014044385A1 (de) | Verfahren zur herstellung von acetylen oder/und ethylen | |
DE19855769B4 (de) | Katalytisch beheizte Komponente für einen chemischen Reaktor | |
DE20321332U1 (de) | Vorrichtung zur Erzeugung von Wasserstoff | |
EP1207134B1 (de) | Gaserzeugungssystem für einen Reformer | |
DE102006019406B4 (de) | Selektiver Oxidations-Reaktor zur Kohlenmonoxidfeinreinigung |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
17P | Request for examination filed |
Effective date: 20060218 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LU MC NL PL PT RO SE SI SK TR |
|
RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: ZARTENAR, NICOLAS Inventor name: WANNINGER, KLAUS Inventor name: BRITZ, PETER Inventor name: WICK, ANJA |
|
DAX | Request for extension of the european patent (deleted) | ||
17Q | First examination report despatched |
Effective date: 20060524 |
|
RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: WANNINGER, KLAUS Inventor name: ZARTENAR, NICOLAS Inventor name: BRITZ, PETER Inventor name: WICK, ANJA |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN |
|
18D | Application deemed to be withdrawn |
Effective date: 20080901 |