EP1651563A1 - Apparatus for producing hydrogen - Google Patents

Apparatus for producing hydrogen

Info

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Withdrawn
Application number
EP04802817A
Other languages
German (de)
French (fr)
Inventor
Nicolas Zartenar
Peter Britz
Klaus Wanninger
Anja Wick
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Viessmann Werke GmbH and Co KG
Sued Chemie AG
Original Assignee
Viessmann Werke GmbH and Co KG
Sued Chemie AG
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Viessmann Werke GmbH and Co KG, Sued Chemie AG filed Critical Viessmann Werke GmbH and Co KG
Publication of EP1651563A1 publication Critical patent/EP1651563A1/en
Withdrawn legal-status Critical Current

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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.

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  • 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

The invention relates to an apparatus for producing hydrogen. Said apparatus comprises a reformer stage (1) for converting hydrocarbon gas and water to hydrogen and other reformed products. At least one of the catalyst stages (2) mounted downstream of the reformer stage (1) is provided for the catalytic conversion of the reformed products. The apparatus also comprises a methanation stage (3) which is mounted downstream of the catalyst stage (2) and through which the medium flows in an axial direction. A flow guidance housing (4) for a coolant extends in the axial direction of flow and is associated with said methanation stage. According to the invention, the flow guidance housing (4) comprises at least two, preferably three or more cooling zones (5, 6, 7, 8) which have different cooling effects and which are disposed one after the other in the axial direction.

Description

( 19 315 ) (19 315)
Apparat zur Erzeugung von WasserstoffApparatus for generating hydrogen
Die Erfindung betrifft einen Apparat zur Erzeugung von Wasserstoff gemäß dem Oberbegriff des Patentanspruchs 1.The invention relates to an apparatus for generating hydrogen according to the preamble of patent claim 1.
Ein Apparat der eingangs genannten Art ist in der vorveröffentlichten DE 202 11 546 Ul und der nachveröffentlichten DE 102 40 953 AI und EP 1 415 705 AI beschrieben. Dieser Apparat besteht u. a. aus einer vorzugsweise mit einem Brenner beheizbaren Dampfreformierstufe zur Umwandlung von Kohlenwasserstoffgas und Wasser in Wasserstoff und weitere Reformer-Produkte wie Kohlendioxid und Kohle monoxid. Mit dem erzeugten Wasserstoff kann beispielsweise eine PEM-Brennstoffzelle betrieben werden. Da das Reformat nach der Reformerstufe noch vergleichweise viel Kohlenmonoxid enthält (Brennstoffzellen- gift) , ist dieser eine Katalysatorstufe nachgeschaltet, um das Kohlenmonoxid katalytisch in Kohlendioxid (unproblematisch für die Brennstoffzelle) umzuwandeln. Zur Feinreinigung, d. h. um den Kohlenmonoxidgehalt im Reformat noch weiter zu senken, ist der Katalysatorstufe schließlich eine sogenannte Methanisie- rungsstufe nachgeschaltet, die das verbliebene Kohlenmonoxid mittels Wasserstoff in Methangas (zurück-) verwandelt. Die Eintrittstemperatur des Kohlenmonoxid enthaltenden Reformatga- ses in die Methanisierungsstufe beträgt dabei in der Regel etwa 240°C. Da der Methanisierungsprozess exotherm abläuft, ist eine Kühlung der Methanisierungsstufe erforderlich. Hierzu ist ein Stromungsfuhrungsgehause für ein Kühlmedium vorgesehen, dass je nach Ausbildung der Methanisierungsstufe wahlweise aussen oder von innen her (beispielsweise bei hohlzylindri- scher Ausbildung) der Stufe zugeordnet ist. Dieses Stromungsfuhrungsgehause ist vom Kühlmedium je nach Bedarf im Gleichoder Gegenstrom zum Reformatstrom durchströmbar.An apparatus of the type mentioned is described in the previously published DE 202 11 546 U1 and the subsequently published DE 102 40 953 AI and EP 1 415 705 AI. This apparatus exists. a. from a steam reforming stage, preferably heated with a burner, for converting hydrocarbon gas and water into hydrogen and further reformer products such as carbon dioxide and carbon monoxide. For example, a PEM fuel cell can be operated with the generated hydrogen. Since the reformate after the reformer stage still contains a comparatively large amount of carbon monoxide (fuel cell poison), this is followed by a catalyst stage in order to catalytically convert the carbon monoxide into carbon dioxide (unproblematic for the fuel cell). For fine cleaning, d. H. Finally, in order to further reduce the carbon monoxide content in the reformate, 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. For this purpose, 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.
Experimente haben nun ergeben, dass das Reformatgas am Austritt der Methanisierungsstufe trotz der beschriebenen Kühlung mittels eines durch das Stromungsfuhrungsgehause geführten Kühlmediums einen unerwartet hohen Kohlenmonoxid-Gehalt auf- weist (100 pp und mehr), der, da das Kohlenmonoxid - wie erwähnt - für die Brennstoffzelle schädlich ist, nicht tolerierbar ist. Ursache für diesen hohen Kohlenmonoxid-Gehalt ist dabei offenbar eine sogenannte Retroshift-Reaktion, bei der der gerade erzeugte Wasserstoff mit dem Reformer-Produkt Kohlendioxid reagiert und dabei Kohlenmonoxid und Wasser bildet. Diese Reaktion ist dabei einerseits aufgrund des Verbrauchs des gerade erzeugten Wasserstoffs, andererseits aber auch wegen der erwähnten schädlichen Wirkung des Kohlenmonoxid auf die Brennstoffzelle unerwünscht.Experiments have now shown that the reformate gas at the outlet of the methanation stage has an unexpectedly high carbon monoxide content, despite the cooling described, by means of a cooling medium passed through the power supply housing. shows (100 pp and more), which, because the carbon monoxide - as mentioned - is harmful to the fuel cell, is intolerable. The reason for this high carbon monoxide content is apparently a so-called retro shift reaction, in which the hydrogen just produced reacts with the reformer product carbon dioxide and thereby forms carbon monoxide and water. This reaction is undesirable on the one hand because of the consumption of the hydrogen just generated, but on the other hand also because of the harmful effect of carbon monoxide on the fuel cell.
Der Erfindung liegt demgemäß die Aufgabe zugrunde, bei einem Apparat der eingangs genannten Art auf möglichst einfache Weise dafür zu sorgen, dass diese Retroshift-Reaktion unterbleibt und der Kohlenmonoxid-Anteil im Reformatgas am Austritt der Methanisierungsstufe möglichst gering ist, vorzugsweise deutlich weniger als 100 ppm beträgt.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.
Diese Aufgabe wird gelöst mit einem Apparat der eingangs genannten Art durch die im Kennzeichen des Patentanspruchs 1 aufgeführten Merkmale.This object is achieved with an apparatus of the type mentioned by the features listed in the characterizing part of patent claim 1.
Nach der Erfindung ist also vorgesehen, dass das Stromungsfuhrungsgehause in Axialrichtung hintereinander angeordnet mindestens zwei, vorzugsweise drei oder mehr Kühlzonen mit unterschiedlicher Kühlwirkung aufweist. Der Einsatz von mindestens zwei Kühlzonen führt zu einem - je nach konstruktiver Ausbildung der Kühlzonen - stufenförmigen oder sich kontinuierlich veränderden Temperaturverlauf innerhalb der Methanisierungsstufe, was bei entsprechender Kühlmediumstemperatur wiederum zur Folge hat, dass trotz des exothermen Methanisierungspro- zesses die Temperatur zum Ausgang der Methanisierungsstufe hin deutlich abnimmt und dementsprechend die unerwünschte Retroshift-Reaktion unterbleibt. Der besondere Vorteil der Erfindung liegt also darin, dass der Temperaturverlauf innerhalb der Methanisierungsstufe gezielt beeinflußbar ist und sich auf diese Weise ein minimaler Kohlenmonoxid-Gehalt im Reformatgas erreichen läßt. Dank der erfindungsgemäßen Lösung kann dabei auch auf ein so¬ genanntes "Air-Bleed" verzichtet werden, dass bisher der Me¬ thanisierungsstufe nach- und der Brennstoffzelle vorgeschaltet war und bei dem mittels geringer Mengen Sauerstoff das rest¬ liche im Reformat enthaltende Kohlenmonoxid oxidiert wurde.According to the invention it is therefore provided that 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. Dan the inventive solution, k may even be dispensed to a so ¬ called "Air Bleed", so far the Me ¬ thanisierungsstufe 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.
Der Vollständigkeit halber wird im Übrigen noch auf die US 3,441,393 A verwiesen, aus der ein Verfahren zur Produktion eines wasserstoffreichen Gases bekannt ist. Bei dieser Anlage ist eine "handelsübliche" Methanisierungsstufe vorgesehen, also keine Gasfeinreinigungsstufe mit der erfindungsgemässen Mehrzonenkühlung. Bei dieser Lösung tritt das Reformatgas mit 316°C in den Methanisierungsreaktor ein und verlässt diesen mit 379°C, d. h. sogar um 63°C erwärmt. Die erfindungsgemäße Erkenntnis, die Methanisierungsstufe mehrstufig zu kühlen, um eine Retroshift-Reaktion zu verhindern, ist dieser Druckschrift nicht zu entnehmen.For the sake of completeness, reference is also made to US 3,441,393 A, from which a method for producing a hydrogen-rich gas is known. In this plant, a "commercially available" methanation stage is provided, that is to say no gas purification stage with the multi-zone cooling according to the invention. In this solution, the reformate gas enters the methanation reactor at 316 ° C and leaves it at 379 ° C, i. H. even warmed by 63 ° C. The knowledge according to the invention of cooling the methanization stage in several stages in order to prevent a retroshift reaction cannot be gathered from this publication.
Aridere vorteilhafte Weiterbildungen der Erfindung ergeben sich aus den abhängigen Ansprüchen.Further advantageous developments of the invention result from the dependent claims.
Der erfindungsgemäße Apparat einschließlich seiner vorteilhaften Weiterbildungen wird nachfolgend anhand der zeichnerischen Darstellung verschiedener Ausführungsbeispiele mit mehreren Diagrammen genauer erläutert.The apparatus according to the invention, including its advantageous further developments, is explained in more detail below with the aid of the graphical representation of various exemplary embodiments with several diagrams.
Es zeigtIt shows
Figur 1 schematisch im Schnitt den erfindungsgemäßen Apparat mit einer Methanisierungsstufe mit vier Kühlzonen;Figure 1 shows schematically in section the apparatus according to the invention with a methanization stage with four cooling zones;
Figur 2 als Diagramm den Temperaturverlauf aufgetragen über der Lauflänge x innerhalb der Methanisierungsstufe bei Verwendung einer Kühlzone (Stand der Technik) ;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);
Figur 3 als Diagramm den Temperaturverlauf aufgetragen über der Lauflänge x innerhalb der Methanisierungsstufe bei Verwendung von vier Kühlzonen; Figur 4 als Diagramm den Temperaturverlauf aufgetragen über der Lauflänge x innerhalb der vier Kühlzonen;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;
Figur 5 schematisch im Schnitt zwei weitere Ausführungsformen des Strömungsführungsgehäuses an der Methanisierungsstufe (der Einfachheit halber in einer Darstellung zusammengefasst) ; undFIG. 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); and
Figur 6 schematisch im Schnitt eine weitere Ausführungsformen des Strömungsführungsgehäuses an der Methanisierungsstufe .Figure 6 shows schematically in section a further embodiment of the flow guide housing at the methanization stage.
In Figur 1 ist der erfindungsgemäße Apparat zur Erzeugung von Wasserstoff schematisch im Schnitt dargestellt.In Figure 1, the apparatus for generating hydrogen according to the invention is shown schematically in section.
Dieser umfasst eine Reformerstufe 1 zur Umwandlung von Kohlen- wasserstoffgas und Wasser in Wasserstoff und weitere Reformer- Produkte. Die einen Reformierkatalysator aufweisende Reformerstufe 1 ist vorzugsweise, wie dargestellt, als mit einem Brenner 9, insbesondere Gasbrenner, beheizte Dampfreformierstufe ausgebildet, d. h. in dieser Stufe wird unter Wärmezufuhr (durch den Brenner 9) beispielsweise CH4 und H20 in CO, CO2 und H2 umgesetzt (endotherme Reaktion) . Um einen möglichst gleichmäßigen Temperaturverlauf innerhalb der Reformerstufe 1 und damit eine optimale Wasserstofferzeugung zu gewährleisten, ist die Reformerstufe 1 vorzugsweise, wie dargestellt, hohlzylin- drisch ausgebildet.This includes a reformer stage 1 for the conversion of hydrocarbon gas and water into hydrogen and other reformer products. 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). In order to ensure that the temperature profile within the reformer stage 1 is as uniform as possible and thus optimal hydrogen generation, the reformer stage 1 is preferably designed as a hollow cylinder, as shown.
Der erfindungsgemäße Apparat umfasst ferner mindestens eine der Reformerstufe 1 nachgeschaltete Katalysatorstufe 2 zur ka- talytischen Konvertierung des Kohlenmonoxids, d. h. dieses wird jedenfalls teilweise in das für die Brennstoffzelle unschädliche Kohlendioxid umgesetzt. Wie bei der Reformerstufe 1 ist auch bei der Katalysatorstufe 2 vorteilhaft vorgesehen, dass diese hohlzylindrisch ausgebildet ist. Diese Maßgabe führt zu einem gleichmäßigeren Temperaturverlauf und damit zu einer besseren Kohlenmonoxidumsetzung innerhalb der Katalysatorstufe 2.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. As with the reformer stage 1, 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.
Schließlich umfasst der erfindungsgemäße Apparat eine der Katalysatorstufe 2 nachgeschaltete, axial durchströmte Methani- sierungsstufe 3, die wie erwähnt dazu dient, möglichst viel des restlichen im Reformatgas enthaltenen Kohlenmonoxids mittels Wasserstoff zu methanisieren. Zur Temperierung der Methanisierungsstufe 3 ist dieser ein sich in axialer Durchströmungsrichtung erstreckendes Stromungsfuhrungsgehause 4 für ein Kühlmedium zugeordnet. Bevorzugt ist die Methanisierungsstufe 3, wie dargestellt, ebenfalls hohlzylindrisc ausgebildet.Finally, the apparatus according to the invention comprises an axially flowing methane downstream of the catalyst stage 2 sierungsstufe 3, which serves, as mentioned, to methanize as much of the remaining carbon monoxide contained in the reformate gas by means of hydrogen. To temper the methanation stage 3, it is assigned a flow guide housing 4, which extends in the axial flow direction, for a cooling medium. As shown, the methanization stage 3 is also preferably of hollow cylindrical design.
Um eine möglichst druckverlustfreie Strömung durch die einzelnen Stufen des erfindungsgemäßen Apparates zu gewährleisten, ist ferner vorteilhaft vorgesehen, dass die Reformerstufe 1, die Katalysatorstufe 2 und die Methanisierungsstufe 3 in axialer Durchströmungsrichtung hintereinander angeordnet sind. Bei hohlzylindrischer Ausbildung ist ferner vorteilhaft vorgesehen, dass die Stufen einen durchgehenden Ringraum definierend in axialer Durchströmungsrichtung hintereinander angeordnet sind.In order to ensure a flow through the individual stages of the apparatus according to the invention that is as free of pressure loss as possible, it is also advantageously provided that the reformer stage 1, the catalyst stage 2 and the methanation stage 3 are arranged one behind the other in the axial flow direction. In the case of a hollow cylindrical design, it is also advantageously provided that the steps are arranged one behind the other defining a continuous annular space in the axial flow direction.
Wesentlich für den erfindungsgemäßen Apparat zur Erzeugung von Wasserstoff ist nun, dass das Stromungsfuhrungsgehause 4 in Axialrichtung hintereinander angeordnet mindestens zwei, vorzugsweise drei und mehr Kühlzonen 5, 6, 7, 8 mit unterschiedlicher Kühlwirkung aufweist.It is essential for the apparatus for generating hydrogen according to the invention that 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.
Bei der Ausführungsform gemäß Figur 1 ist das Stromungsfuhrungsgehause 4 in vier Kühlzonen 5, 6, 7, 8 aufgeteilt, denen das Kühlmedium jeweils separat zuführbar ist. Prinzipiell eignen sich aber bereits zwei Zonen zur Lösung der eingangs definierten Aufgabe. Je mehr Kühlzonen vorgesehen werden, desto genauer läßt sich zwar der Temperaturverlauf innerhalb der Methanisierungsstufe festlegen, desto größer ist aber auch der apparative Aufwand. Vier Zonen haben sich hier als eine günstige Auswahl erwiesen.In the embodiment according to FIG. 1, 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. In principle, however, 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.
Bei hohlzylindrischer Ausbildung der Methanisierungsstufe 3 hat es sich ferner als vorteilhaft erwiesen, dass die Kühlzonen 5, 6, 7, 8 wahlweise innen und/oder aussen an der Methanisierungsstufe 3 angeordnet sind (siehe Figur 6) . Dabei umschliessen die Kühlzonen 5, 6, 7, 8 vorzugsweise wie axial hintereinander angeordnete Ringräume die Methanisierungsstufe 3 bzw. sind bei hohlzylindrischer Ausbildung von der Methani- sierung-sstufe 3 von dieser umschlossen (siehe wiederum Figur 6).In the case of a hollow cylindrical configuration of the methanation stage 3, it has also proven to be advantageous that the 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).
Wie in Figur 1 schematisch dargestellt, ist ferner vorteilhaft vorgesehen, dass jede Kühlzone 5, 6, 7, 8 jeweils mindestens einen Kühlmittelzu- 10 und einen Kühlmittelabfuhranschluss 11 aufweist, wobei jede Kühlzone 5, 6, 7, 8 ferner vorteilhaft vom Kuhlmedium wahlweise im Gleich- (nicht dargestellt) oder Gegenstrom zur Methanisierungsstufe 3 durchströmbar ist.As shown schematically in FIG. 1, it is also advantageously provided that 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.
Um ferner eine optimale, bedarfsangepaßte Kühlung zu realisieren, ist vorteilhaft vorgesehen, dass den Kühlzonen 5, 6, 7, 8 unterschiedliche Kühlmedien zugeführt werden.In order to further realize an optimal, customized cooling, it is advantageously provided that the cooling zones 5, 6, 7, 8 are supplied with different cooling media.
Ferner ist vorteilhaft vorgesehen, dass wahlweise das eine verwendete Kühlmedium mit unterschiedlichen Temperaturen den einzelnen Zonen 5, 6, 7, 8 zugeführt wird oder dass bei Verwendung- unterschiedlicher Kühlmedien diese selbst unterschiedlich temperiert sind, und zwar beispielsweise durch den Einsatz nicht dargestellter Wärmetauscher.Furthermore, it is advantageously provided that either the 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).
In Ficjur 2 ist ein Temperaturverlauf über der Lauflänge x (siehe Figur 1) innerhalb einer Methanisierungsstufe dargestellt, die lediglich über eine Kühlzone verfügt (Stand der Technik) . Wie erwähnt, wird in der Methanisierungsstufe Kohlenmonoxid und Wasserstoff in Kohlenwasserstoffgas (Methan) zurückverwandelt, um den Kohlenmonoxidanteil im Reformatgas zu reduzieren. Da die Methanisierung ein exothermer Vorgang ist, steigt die Temperatur in der Stufe zunächst an und fällt dann aufgrund der Kühlung auf einen Wert knapp unterhalb der Eintrittstemperatur ab. Der Kohlenmonoxidgehalt beträgt bei einer derartigen Konstruktion üblicherweise etwa 120 ppm, also zuviel , um das Reformatgas direkt zur Brennstoffzelle zu leiten. Wie erwähnt, ist deshalb der Methanisierungsstufe in der Regel ein "Air-Bleed" nachgeschaltet, um auch noch diesen Anteil an Kohlenmonoxid zu entfernen. Als Ursache für den doch noch vergleichweise hohen Kohlen- monoxidanteil im Reformatgas nach der Methanisierungsstufe hat sich herausgestellt, dass es aufgrund der recht hohen Temperaturen zum Ausgang der Stufe hin immer wieder zu sogenannten Retroshift-Reaktionen kommt, bei denen Kohlendioxid und Wasserstoff zu Kohlenmonoxid und Wasser reagiert.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). As mentioned, 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. Since 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. With such a construction, the carbon monoxide content is usually about 120 ppm, that is too much to direct the reformate gas directly to the fuel cell. As mentioned, the methanation stage is therefore usually followed by an "air bleed" in order to also remove this proportion of carbon monoxide. The reason for the still comparatively high proportion of carbon monoxide in the reformate gas after the methanation stage has been found to be the so-called retro-shift reactions due to the rather high temperatures at the exit of the stage, in which carbon dioxide and hydrogen become carbon monoxide and water responding.
Nach der Erfindung ist nun, wie beschrieben, vorgesehen, die Methanisierungsstufe in mehrere Kühlzonen aufzuteilen, um gezielt zum Ausgang der Stufe hin die Temperatur derart abzusenken, dass es nicht mehr zu der unerwünschten Retroshift-Reaktion ko mmt. In Figur 3 ist ein entsprechender Temperaturverlauf dargestellt, der sich beim Einsatz der erfindungsgemäßen Kühlzonenaufteilung einstellen lässt. Die Temperatur in der Methanisierungsstufe fällt bei dieser Lösung also kontinuierlich von 240°C auf etwa 220°C ab, mit dem Ergebnis, das insbesondere am Ende der Methanisierungsstufe keine Retroshift-Reaktion mehr erfolgen kann, da dazu die Temperturen im Bereich dieser Kühlzone zu niedrig sind. Die Bezugszeichen 5, 6, 7, 8 und die gepunkteten Linien in Figur 3 sollen den An- ordnungsbereich der Kühlzonen verdeutlichen.According to the invention, as described, there is now provision for dividing the methanation stage into a plurality of cooling zones in order to lower the temperature in a targeted manner towards the exit of the stage in such a way that the undesired retroshift reaction no longer occurs. 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.
In Figur 4 ist der Temperaturverlauf innerhalb der einzelnen Kühlzonen dargestellt. Es fällt insbesondere auf, dass aufgrund der Kühlung im Gegenstrom eine Art Sägezahnprofil entsteht, aber die Temperaturspitzen zum Ausgang der Stufe immer weiter abfallen, woraus sich zwangsläufig auf den gewünschten, abfallenden Temperaturverlauf innerhalb der Methanisierungsstufe schließen läßt.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.
Gemäß der in Figur 5 dargestellten zwei weiteren Ausführungsformen des Strömungsführungsgehäuses 4 der Methanisierungsstufe ist alternativ zur Lösung gemäß Figur 1 vorgesehen, dass die in Axialrichtung hintereinander angeordneten Kühlzonen 5, 6, 7, 8 unmittelbar hydraulisch miteinander verbunden sind, aber unterschiedliche Durchströmungsquerschnitte aufweisen. Erfindungsgemäß ist somit eine unmittelbare hydraulische Trennung der Kühlzonen 5, 6, 7, 8 nicht zwingend, vielmehr kann auch durch geeignete Wahl der axialen Durchströmsquerschnitte die wärmeüber-tragung in den einzelnen Bereichen der Methanisierungsstufe gezielt beeinflusst werden. Dabei gilt: Großer Durchströmungsquerschnitt, kleine Strömungsgeschwindigkeit und somit relativ schlechte Wärmeübertragung, oder kleiner Querschnitt, große Strömungsgeschwindigkeit und damit recht gute Wärmeübertragung; alles natürlich auch in Abhängigkeit vom Temperaturgefälle zwischen Kühlmedium und Methanisierungsstufe.According to the two further embodiments of the flow guide housing 4 of the methanation stage shown in FIG. 5, as an alternative to the solution according to FIG. 1, it is provided that 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. According to the invention, 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 following applies: large flow cross-section, low flow velocity and thus relatively poor heat transfer, or small cross-section, large flow velocity and therefore quite good heat transfer; all of course also depending on the temperature gradient between the cooling medium and the methanation stage.
Gemäß der oberen Darstellung in Figur 5 ist schließlich vorteilhaft vorgesehen, dass die Kühlzonen 5, 6, 7, 8 in Axialrichtung zueinander gestufte Durchströmungsquerschnitte aufweisen. Alternativ (untere Darstellung) sind aber auch sich kontinuierlich verändernde Durchströmungsquerschnitte vorgesehen, wobei in beiden Fällen die Kühlzonen 5, 6, 7, 8 vom Kühlmedium wahlweise im Gleich- oder Gegenstrom zur Methanisierungsstufe 3 durchströmbar sind. Finally, according to the upper illustration in FIG. 5, it is advantageously provided that the cooling zones 5, 6, 7, 8 have flow cross sections that are stepped in the axial direction. Alternatively (bottom illustration), however, 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.
( 19 315 )(19 315)
BezugszeichenlisteLIST OF REFERENCE NUMBERS
1 Reformerstufe1 reform stage
2 Katalysatorstufe2 catalyst stage
3 Methanisierungsstufe3 methanation level
4 Stromungsfuhrungsgehause4 power supply housing
5 Kühlzone5 cooling zone
6 Kühlzone6 cooling zone
7 Kühlzone7 cooling zone
8 Kühlzone8 cooling zone
9 Brenner9 burners
10 Kühlmittelzufuhranschluss10 coolant supply connection
11 Kühlmittelabfuhranschluss 11 Coolant discharge connection

Claims

( 19 315 )(19 315)
Patentansprücheclaims
1. Apparat zur Erzeugung von Wasserstoff, umfassend a) eine Reformerstufe (1) zur Umwandlung von Kohlenwasserstoffgas und Wasser in Wasserstoff und weitere Reformer-Produkte wie Kohlendioxid und Kohlenmonoxid, b) mindestens eine der Reformerstufe (1) nachgeschaltete Katalysatorstufe (2) zur katalytischen Konvertierung des beim Reformierungsprozess entstandenen Kohlenmono- xids, c) eine der Katalysatorstufe (2) nachgeschaltete, axial durchströmte Methanisierungsstufe (3), der ein sich in axialer Durchströmungsrichtung erstreckendes Stromungsfuhrungsgehause (4) für ein Kühlmedium zugeordnet ist, dadurch gekennzeichnet, dass das Stromungsfuhrungsgehause (4) in Axialrichtung hintereinander angeordnet mindestens zwei, vorzugsweise drei und mehr Kühlzonen (5, 6, 7, 8) mit unterschiedlicher Kühlwirkung auf e st.1. Apparatus for generating hydrogen, comprising a) a reformer stage (1) for converting hydrocarbon gas and water into hydrogen and further reformer products such as carbon dioxide and carbon monoxide, b) at least one catalyst stage (2) downstream of the reformer stage (1) for catalytic Conversion of the carbon monoxide formed during the reforming process, c) a methanation stage (3) downstream of the catalyst stage (2) and with which a flow guide housing (4) for a cooling medium extending in the axial direction of flow is assigned, characterized in that the flow guide housing ( 4) arranged in the axial direction one behind the other at least two, preferably three and more cooling zones (5, 6, 7, 8) with different cooling effects on e st.
2. Apparat zur Erzeugung von Wasserstoff nach Anspruch 1, dadurch gekennzeichnet, dass den Kühlzonen (5, 6, 7, 8) das Kühlmedium jeweils separat zuführbar ist.2. Apparatus for generating hydrogen according to claim 1, characterized in that the cooling zones (5, 6, 7, 8), the cooling medium can be fed separately.
3. Apparat zur Erzeugung von Wasserstoff nach Anspruch 2, dadurch gekennzeichnet, dass die Kühlzonen (5, 6, 7, 8) wie axial hintereinander angeordnete Ringräume die Methanisierungsstufe (3) um- schliessen bzw. bei hohlzylindrischer Ausbildung der Methanisierungsstufe (3) von dieser umschlossen sind. Apparat zur Erzeugung von Wasserstoff nach Anspruch 2 oder3. Apparatus for the production of hydrogen according to claim 2, characterized in that the cooling zones (5, 6, 7, 8) like annular spaces arranged axially one behind the other surround the methanation stage (3) or, in the case of a hollow cylindrical formation of the methanization stage (3) these are enclosed. Apparatus for generating hydrogen according to claim 2 or
3, dadurch ge ennzeichnet , dass jede Kühl zone (5, 6, 7, 8) jeweils mindestens einen3, characterized in that each cooling zone (5, 6, 7, 8) each has at least one
Kühlmittelzu- (10) und einen Kühlmittelabfuhranschluss (11) aufweist.Coolant supply (10) and a coolant discharge connection (11).
Apparat zur Erzeugung von Wasserstoff nach einem der Ansprüche 2 bis 4, dadurch ge ennzeichnet, dass jede Kühlzone (5, 6, 7, 8) vom Kühlmedium wahlweise im Gleich- oder GJegenstrom zur Methanisierungsstufe (3) durchströmbar ist.Apparatus for generating hydrogen according to one of claims 2 to 4, characterized in that each cooling zone (5, 6, 7, 8) can be flowed through by the cooling medium either in cocurrent or countercurrent to the methanation stage (3).
Apparat zur Erzeugung von Wasserstoff nach einem der Ansprüche 2 bis 5, dadurch ge ennzeichnet, dass den Kühlzonen (5, 6, 7, 8) unterschiedliche, vorzugsweise unterschiedlich temperierte Kühlmedien zuführbar sind.Apparatus for generating hydrogen according to one of claims 2 to 5, characterized in that the cooling zones (5, 6, 7, 8) can be supplied with different, preferably differently tempered cooling media.
Apparat zur Erzeugung von Wasserstoff nach Anspruch 1, dadurch ge ennzeichnet, dass die in Axialrichtung hintereinander angeordneten Kühlzonen (5, 6, 7, 8) unmittelbar hydraulisch miteinander verbunden sind, aber unterschiedliche Durchströmungsquerschnitte aufweisen, wobei die Kühlzonen (5, 6, 7, 8) vorzugsweise in Axialrichtung wahlweise zueinander gestufte oder sich kontinuierlich verändernde Durchströmungsquerschnitte aufweisen und wobei die Kühlzonen (5, 6, 7, 8) vorzugsweise vom Kühlmedium wahlweise im Gleich- oder Gegenstrom zur Methanisierungsstufe (3) durchströmbar sind. Apparatus for generating hydrogen according to claim 1, characterized in that 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, the cooling zones (5, 6, 7, 8) preferably have flow cross sections which are either stepped or continuously changing in the axial direction, and the cooling zones (5, 6, 7, 8) can preferably be flowed through by the cooling medium either in cocurrent or countercurrent to the methanation stage (3).
8. Apparat zur Erzeugung von Wasserstoff nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, dass die Reformerstufe (1) , vorzugsweise die Katalysatorstufe (2) und vorzugsweise die Methanisierungsstufe (3) hohlzylindrisch ausgebildet ist.8. Apparatus for generating hydrogen according to one of claims 1 to 7, characterized in that the reformer stage (1), preferably the catalyst stage (2) and preferably the methanization stage (3) is hollow-cylindrical.
9. Apparat zur Erzeugung von Wasserstoff nach Anspruch 8 , dadurch gekennzeichnet, dass die Reformerstufe (1), die Katalysatorstufe (2) und die Methanisierungsstufe (3) bei hohlzylindrischer Ausbildung einen durchgehenden Ringraum definierend in axialer Durchströmungsrichtung hintereinander angeordnet sind9. Apparatus for generating hydrogen according to claim 8, characterized in that the reformer stage (1), the catalyst stage (2) and the methanization stage (3) are arranged one behind the other in a hollow cylindrical configuration defining a continuous annular space in the axial flow direction
10. Apparat zur Erzeugung von Wasserstoff nach Anspruch 8 oder 9, dadurch ekennzeichnet, dass die Kühlzonen (5, 6, 7, 8) bei hohlzylindrischer Ausbildung der Methanisierungsstufe (3) wahlweise innen und/oder aussen an der Methanisierungsstufe (3) angeordnet sind. 10. Apparatus for generating hydrogen according to claim 8 or 9, characterized in that the cooling zones (5, 6, 7, 8) are arranged inside and / or outside on the methanization stage (3) with a hollow cylindrical configuration of the methanation stage (3) ,
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Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5037878B2 (en) * 2006-08-25 2012-10-03 日本碍子株式会社 Permselective membrane reactor and method for producing hydrogen gas
EP2602228B1 (en) * 2010-08-03 2017-11-08 Panasonic Intellectual Property Management Co., Ltd. Hydrogen generation device and fuel cell system
JP6194143B2 (en) * 2013-09-09 2017-09-06 千代田化工建設株式会社 Hydrogen and synthetic natural gas production apparatus and production method
WO2015033583A1 (en) * 2013-09-09 2015-03-12 千代田化工建設株式会社 Manufacturing device and manufacturing method for hydrogen and synthetic natural gas

Family Cites Families (17)

* Cited by examiner, † Cited by third party
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 (en) * 2002-03-25 2003-10-16 Viessmann Werke Kg Device for producing hydrogen has conversion stages and fine purification stage formed as hollow bodies having an annular chamber for receiving corresponding catalysts
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 (en) * 1998-03-05 2005-12-07 三洋電機株式会社 CO removal apparatus and method of operating CO removal apparatus
JP2000185901A (en) * 1998-12-21 2000-07-04 Aisin Seiki Co Ltd Reforming device and fuel battery system
JP2000256003A (en) * 1999-03-08 2000-09-19 Osaka Gas Co Ltd Method for removing co in hydrogen enriched gas
JP3772619B2 (en) * 1999-12-28 2006-05-10 松下電器産業株式会社 Hydrogen generator
KR100427165B1 (en) * 1999-12-28 2004-04-14 마쯔시다덴기산교 가부시키가이샤 Hydrogen generator
DE10057537A1 (en) * 2000-11-20 2002-06-06 Viessmann Werke Kg Device for producing hydrogen used for operating fuel cells comprises a reformer for converting hydrocarbon gas and water into hydrogen and further reformer products connected to a heat
JP4285992B2 (en) * 2000-12-13 2009-06-24 テキサコ ディベラップメント コーポレイション Single chamber compact fuel processor
JP2002282690A (en) * 2001-03-26 2002-10-02 Osaka Gas Co Ltd Catalyst for removing carbon monoxide, method for removing carbon monoxide, and reactor for removing carbon monoxide
JP3853632B2 (en) * 2001-10-26 2006-12-06 三菱電機株式会社 Carbon monoxide remover for fuel cell power generator and operation method
KR100596191B1 (en) * 2002-03-15 2006-07-06 마츠시다 덴코 가부시키가이샤 Reforming Apparatus and Operation Method Thereof
WO2003080505A1 (en) * 2002-03-25 2003-10-02 Viessmann Werke Gmbh & Co. Kg Device for the generation of hydrogen
JP2003277013A (en) * 2002-03-27 2003-10-02 Osaka Gas Co Ltd Carbon monoxide removing method and polymer electrolyte fuel cell system
DE10250793A1 (en) * 2002-10-30 2004-05-19 Viessmann Werke Gmbh & Co Kg Apparatus for generating hydrogen and method for operating such an apparatus

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2005054125A1 *

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US20080019884A1 (en) 2008-01-24
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WO2005054125A1 (en) 2005-06-16
DE10356650A1 (en) 2005-07-07

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