WO2003024867A1 - Kompakte reformereinheit zur wasserstofferzeugung aus gasförmigen kohlenwasserstoffen im kleinen leistungsbereich - Google Patents
Kompakte reformereinheit zur wasserstofferzeugung aus gasförmigen kohlenwasserstoffen im kleinen leistungsbereich Download PDFInfo
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- WO2003024867A1 WO2003024867A1 PCT/DE2002/003064 DE0203064W WO03024867A1 WO 2003024867 A1 WO2003024867 A1 WO 2003024867A1 DE 0203064 W DE0203064 W DE 0203064W WO 03024867 A1 WO03024867 A1 WO 03024867A1
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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- 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
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- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
- B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/10—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically
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- 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
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00141—Coils
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00504—Controlling the temperature by means of a burner
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- 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
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- 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
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- 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
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- 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
- C01B2203/0288—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step containing two CO-shift steps
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- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/047—Composition of the impurity the impurity being carbon monoxide
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- C01B2203/066—Integration with other chemical processes with fuel cells
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- 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
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- C01B2203/08—Methods of heating or cooling
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- 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
- C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
- C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
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- C01B2203/08—Methods of heating or cooling
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- C01B2203/1005—Arrangement or shape of catalyst
- C01B2203/1023—Catalysts in the form of a monolith or honeycomb
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- C01B2203/1047—Group VIII metal catalysts
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- C01B2203/14—Details of the flowsheet
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- C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
- C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus
Definitions
- the invention relates to a compact
- Steam reformer which generates a hydrogen-rich product gas from hydrocarbons or hydrocarbon derivatives with the addition of water, and a method for producing the hydrogen-containing product gas.
- the product gas can e.g. be used in a fuel cell where electricity and heat are generated.
- the device according to the invention is preferably suitable for producing a hydrogen-containing product gas for supplying fuel cells in the stationary, decentralized power range.
- the plant sizes range from power generation in the MW range to cogeneration plants with a few hundred kW for cogeneration, up to an electrical output of 1 - 10 kW for the individual supply of single and multi-family houses.
- the plant sizes range from power generation in the MW range to cogeneration plants with a few hundred kW for cogeneration, up to an electrical output of 1 - 10 kW for the individual supply of single and multi-family houses.
- the Steam reformer used either a radiant burner or a burner with one or more point heat sources.
- the flue gas and the product gas are conducted in countercurrent to the educt flow.
- the internal heat flows of the steam reformer are connected according to the invention in such a way that no cooling lines or further heating are necessary for regulating the temperature levels.
- a steam-containing product gas can be produced by steam reforming hydrocarbons, in particular methane as the main constituent of natural gas.
- the hydrogen-rich gas mixture still contains a carbon monoxide content of about 0.5-1%.
- the heat required for reforming is passed through a central burner, that of a ceramic tube is provided.
- the hot flue gas flows in an annular gap between the burner tube and a second reforming chamber arranged concentrically to it, the flue gas and starting material (fuel gas / water vapor mixture) being conducted in cocurrent.
- the flue gas transfers additional heat in countercurrent to the educt mixture, which flows through a first reforming chamber which is arranged concentrically with the second reforming chamber and is connected to it in terms of flow technology.
- a radiant burner is used in order to heat the surface of the reforming reactor, which is made up of two parts, from the outside.
- the reforming reactor consists of an inner tubular reactor and an annular gap reactor surrounding it at a distance.
- the hot flue gas is conducted in the gap between the tubular reactor and the annular gap reactor in countercurrent to the natural gas in the tubular reactor.
- the educts are fed to the tubular reactor through a heat exchanger designed as a spiral tube, and are heated there by the flue gas conducted in countercurrent. It is not intended to use the sensible heat of the hydrogen-containing product gas and to integrate shift stages in the reformer.
- the object of the invention is therefore to provide an improved method and a plant for producing hydrogen-containing product gas in the small output range.
- the object of the invention is achieved by providing a compact and efficient steam reforming reactor for use in decentralized fuel line systems in the low power range and a method, preferably using the steam reforming reactor according to the invention.
- the present invention therefore relates to a
- Reforming unit for generating hydrogen from a starting material from a hydrocarbon-water mixture, comprising: a reactor vessel; a feed line for feeding a starting material into the reactor vessel; a heat exchanger connected to the starting material feed line with a first pipe connected to the feed line and a second pipe; a further heat exchanger connected to the first tube of the heat exchanger and arranged around a reforming room; a line connected to the heat exchanger with at least one outlet opening for feeding the gaseous starting material into the reforming room with a catalyst unit arranged therein which can be heated by a burner; at least one discharge line for discharging the reformate formed in the reforming room to the second tube of the heat exchanger, which is connected at the other end to a shift reactor; and a product discharge line for the product gas discharged from the shift reactor and at least one discharge line for the flue gas from the reactor vessel.
- the steam reforming reactor according to the invention has a compact construction volume, with all reactors and heat exchangers being accommodated in one housing.
- the efficiency of the hydrogen production (lower calorific value of the hydrogen produced based on the lower calorific value of the fuel for reforming and burner supply) of the reformer in nominal load operation is approx. 80% and is therefore of the order of magnitude of large-scale plants for hydrogen production.
- the present invention also relates to a process for the production of hydrogen from gaseous hydrocarbons, in which a starting material from a hydrocarbon gas / water mixture is passed into a reactor vessel via a feed line into a first one located in the reactor vessel
- Counterflow heat exchanger is supplied, the educt gas mixture emerging from the first heat exchanger is fed to a second heat exchanger for further heating, the further heated educt gas discharged from the second heat exchanger is supplied to a reforming room with a reformer arranged therein Catalyst unit and a burner, which is operated with fuel gas and oxygen / air, is fed, the reformate discharged from the reforming room via a discharge line is fed to the first heat exchanger and is fed in the counterflow direction to the feed material fed to a low-temperature shift reactor and the product gas discharged from the low-temperature shift reactor is discharged from the reactor vessel.
- the product gas is removed via a fine cleaning stage, as a result of which the carbon monoxide content in the product gas is further reduced.
- a special feature of the method according to the invention is that, in a preferred embodiment, the starting material is passed in countercurrent both to the reformate discharged from the reforming chamber and in countercurrent to the flue gas discharged from the combustion chamber.
- a coaxial heat exchanger is therefore preferably used in the method according to the invention, which has a first outer tube and a second inner tube which is surrounded by the outer tube.
- the educt-water mixture is directed towards the reforming room, while in the inner tube, the reformate is led from the reforming room to the shift reactor.
- the hot flue gas is applied to the outer wall of the outer tube, so that intensive heat transfer takes place on both sides to the educt-water mixture to be heated.
- the shift reactor can be used as a low-temperature shift reactor, usually in the temperature range between 180 ° and 250 ° C is operated, or depending on the conditions as a high-temperature shift reactor, which is usually operated in the temperature range between 350 ° and 500 ° C.
- the design as a low-temperature shift reactor is preferred.
- Liquid water and fuel gas are supplied as educt to the steam reformer, and the burner is supplied with air and fuel gas. Flue gas and product gas are discharged as products.
- the hot flue gas primarily serves to provide the endothermic heat of reaction of the reforming reactions.
- both the sensible heat of the hot flue gas and the reformate are used to preheat the starting materials (fuel gas and liquid water) in the further course of the flow.
- the internal heat flows are coupled in such a way that no cooling pipes or additional heating is required to control the temperature levels.
- the regulation takes place via the metering of the educt streams: the reformer temperature is regulated via the combustion output and the shift temperature within the limits via the steam-to-carbon (S / C) ratio.
- the S / C ratio is preferably 2-4, particularly preferably 3.
- an upper region and a lower region are provided in the reaction container, the lines for supplying the starting material and also for removing the product gas and the flue gas being provided in the upper region.
- the feed line is preferably directly with the connected first heat exchanger, which is preferably arranged spirally for heat exchange around the shift reactor.
- the heated product gas is fed from the lower end of the first heat exchanger to a second heat exchanger, in which the heat exchange only takes place between the flue gas discharged from the burner chamber and the already heated product gas located in the interior of the second heat exchanger.
- the further heated feed gas is led into the space around the burner, where the feed gas is released from the feed line into the space around the burner and is subjected to the reforming in the catalyst unit.
- the catalyst unit there is preferably a cavity from which a discharge line of the reformate, which is preferably arranged in the middle, is fed to the inner tube of the first tube exchanger and is conducted in countercurrent to the starting material supplied.
- Steam reformer as a unit consisting of reformer, reformer burner, shift reactor and optional CO gas fine cleaning can be implemented in the power range from 500 watts to 50 kW.
- home energy supply systems can be implemented in the power range from 500 watts to 50 kW.
- Electricity and heat supply for households are shown. With regard to the dimensions, the entire system can be integrated into a wall heater.
- a radiant burner with one or more point-shaped heat sources is used in the embodiment of the steam reformer according to the invention.
- a concentric arrangement lends itself to this, the heat input being realized by radiation and convection. Flue gas and starting material mixture (fuel gas and water) are conducted in counterflow.
- the reaction temperature reached largely determines the conversion of the reformer fuel used, on the one hand due to the position of the thermodynamic equilibrium and on the other hand through the increase in the reaction rate, and has a massive effect on the efficiency.
- the reformer temperature can be regulated by the burner output. By combining heat transfer by radiation and convective heat transfer of the flue gas in countercurrent to the educt flow (fuel gas / water vapor mixture), a sufficiently high reaction temperature can be set in the upper area of the reformer catalyst with the lowest possible burner output.
- the efficiency of a steam reformer strongly depends on the ratio of the fuel gas flow for reforming to the gas flow required for the burner. The higher this ratio, the higher the efficiency of the reformer system.
- the starting material fuel and water
- the starting material is preheated, in the case of a coaxial heat exchanger in an annular gap, simultaneously by cooling the reformate from the inside (from about 700 ° C. to 200 ° C.) and by lowering the flue gas temperature on the outside.
- a coaxial heat exchanger coil is therefore preferably provided in the construction according to the invention.
- the hot reformate is conducted in the inner tube, the cold starting material mixture in the intermediate space and the hot flue gas around the helix, where countercurrent and cocurrent flow are possible.
- the heat exchanger coil can preferably be arranged in a space-saving manner around a low-temperature shift reactor. This allows cooling of this reactor at the same time.
- the present invention therefore relates, as an important element of the invention, also to a countercurrent heat exchanger with 1. a heat exchanger consisting of an inner tube for receiving a heat-emitting fluid and an annular gap tube surrounding the inner tube for receiving the fluid to be heated, also referred to as a spiral double tube or coaxial heat exchanger, and 2. an outer tube surrounding the heat exchanger, the starting material in the annular gap tube in countercurrent to that in the inner tube
- Coaxial heat exchanger surrounding outer tube formed in the form of the reactor vessel.
- the coaxial heat exchanger preferably with coaxially spaced turns in the reactor vessel, is preferably arranged such that the hot flue gas discharged from the burner chamber flows around the coaxial heat exchanger at least in the spiral double tube intermediate space.
- the spiral double tube is arranged around a shift reactor, which is preferably designed as a low-temperature shift reactor.
- this is designed in the form of a countercurrent heat exchanger with a hollow cylinder block with two hollow cylinders, which have a different diameter and are inserted into one another with the same axial length, and with a spiral tube for
- the cylindrical annular gap between the hollow cylinders is closed at both ends by an annular end plate, and in the end plates there are at least one inlet or outlet for the fluids guided in countercurrent into the spiral tube or the cylindrical annular gap.
- an outer tube with feed and discharge is provided for receiving a further heat-emitting fluid, feeds and discharges for the heat-emitting fluids and the heat-absorbing fluid being provided in the respective compartments and the fluid to be heated being in the annular gap tube is led in countercurrent to both heat-emitting fluids.
- the hot flue gas is applied to the outside of the hollow cylinder block, which leads to a further heat exchange with the inside of the double cylinder.
- an HT shift reactor for reducing the construction volume and for simplifying the heat integration can preferably be dispensed with.
- the heat otherwise distributed over two reactors is released in one reactor and can be better used. If the high-temperature shift is omitted, the control of the system is also simplified, since one temperature value has to be monitored and regulated less.
- a bypass line must be provided around the NT shift reactor due to the removal of the initial sulfur loading, so that the NT shift catalyst is not poisoned. This additional line and corresponding regulation can be dispensed with in the described preferred embodiment of the steam reformer.
- Fig.l is a schematic representation of the reforming unit for hydrogen production by steam reforming hydrocarbons
- FIG. 2 shows a schematic representation of the heating of the educt mixture by the hot flue gas and product gas (reformate) according to the invention
- the cylindrical reforming unit 1 has an educt inlet line 2. Via the line 2, the hydrocarbon and liquid water to be reformed are passed into the annular gap 3a of the coaxial heat exchanger 3 in a preset S / C ratio.
- the coaxial heat exchanger coil 3 is arranged concentrically around the low-temperature shift reactor 4.
- the hot reformate coming from the reformer area is conducted in countercurrent to the starting material mixture, while the hot flue gas flows around the coaxial heat exchanger coil.
- the preheating and evaporation of the reactants in the coaxial heat exchanger thus takes place in the
- the educt mixture is conducted in countercurrent with respect to both the reformate and the flue gas.
- the starting material After flowing through the coaxial heat exchanger coil 3, the starting material is in a further tube coil 5, which is concentric around the Reforming room 6 and burner 7 is arranged, directed.
- the starting material mixture is further heated by the hot flue gas flowing in countercurrent on the outside of the coiled tubing and passed through the gas distributor pipe 8 into the reforming chamber 6.
- the reformed starting materials After flowing through the reforming chamber 6, the reformed starting materials reach the upper reformer area and are drawn off via the pipeline 9 and fed to the inner tube 3b of the coaxial heat exchanger coil 3.
- the reforming space 6 is here preferably designed as a concentric annular gap around the burner 7, which is directed upwards through a dome, e.g. is limited in the form of a dished bottom, or in the form of a flat circular disc.
- the cross section of the upper reformer area is circular.
- a free volume 10 is provided for uniform gas distribution over the flow cross section. This can be done constructively through a sieve tray that carries the catalyst material.
- the reforming area can be subdivided into a pre-reforming area and a main reforming area, in which different catalysts which are active in the prevailing temperatures can be used.
- the different catalysts can also be separated by catalytically inactive blind beds or by additional sieve trays. Due to this temperature distribution, the prereformer is used in the inlet area and the main reformer in the outlet area.
- Both catalysts can contain Pt or Ni, for example, and consist of a bed or a coated honeycomb.
- the pipeline 9 can be arranged centrally in the middle of the upper reformer area or else radially.
- Natural gas, or a hydrogen-containing anode exhaust gas from a fuel cell, and air are fed to the burner 7 via a fuel gas supply and air supply, not shown.
- the flue gas generated during combustion is used to heat the reforming room.
- the cylindrical reforming unit 1 and the reformer area 6 are preferably provided with an insulation layer for thermal insulation.
- the coaxial heat exchanger coil 3 consists of an inner tube 3b in which the reformate leaving the reformer 6 is cooled and an outer tube 3a which carries the cold starting material (hydrocarbon-water mixture). Flue gas flows around the outer pipe 3b, which leads to additional preheating of the starting material.
- This double heat exchange of the starting material mixture for the hydrogen-containing reformate and for the flue gas can take place in cocurrent or preferably in countercurrent.
- the advantage of the construction shown is a small size.
- FIG. 1 Although a reforming unit with a reformer and a subsequent low-temperature shift reactor, which is usually operated in the temperature range between 180.degree. And 250.degree. C., is shown in FIG. 1, it is also possible according to the invention, or depending on the circumstances, between the
- Reformer and the low-temperature shift reactor another shift reactor, which as a low-temperature or high-temperature shift reactor, which is usually in the Temperature range between 350 ° and 500 ° C is operated, can be provided.
- reformate is passed from the reforming room into this first shift reactor and directed in countercurrent to the preheated starting material to the low-temperature shift reactor, the guidance of starting material, reformate and flue gas preferably being carried out as shown above in the case of the low-temperature shift reactor.
- Reforming unit 1 reactant inlet line 2 coaxial heat exchanger 3 with annular gap tube 3a and inner tube 3b shift reactor 4 coil 5, reforming chamber 6 burner 7
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- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- General Health & Medical Sciences (AREA)
- Health & Medical Sciences (AREA)
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- Thermal Sciences (AREA)
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Abstract
Description
Claims
Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP02769879A EP1425244B1 (de) | 2001-09-03 | 2002-08-22 | Kompakte reformereinheit zur wasserstofferzeugung aus gasformigen kohlenwasserstoffen im kleinen leistungsbereich |
KR1020047003161A KR100848047B1 (ko) | 2001-09-03 | 2002-08-22 | 낮은 전원 범위에서 기상 탄화수소로부터 수소를 생성하기위한 고효율, 소형 개질 장치 |
DE50209935T DE50209935D1 (de) | 2001-09-03 | 2002-08-22 | Kompakte reformereinheit zur wasserstofferzeugung aus gasformigen kohlenwasserstoffen im kleinen leistungsbereich |
US10/488,439 US7803202B2 (en) | 2001-09-03 | 2002-08-22 | Reformer unit for generating hydrogen from a starting material comprising a hydrocarbon-water mixture |
DK02769879T DK1425244T3 (da) | 2001-09-03 | 2002-08-22 | Kompakt reformerenhed til produktion af hydrogen fra gasholdige carbonhydrider i det lave ydelsesområde |
JP2003528722A JP4504016B2 (ja) | 2001-09-03 | 2002-08-22 | 低パワーレンジにおいてガス状炭化水素から水素を生成するための高効率かつコンパクトなリフォーマ・ユニット |
CA2459429A CA2459429C (en) | 2001-09-03 | 2002-08-22 | Highly efficient, compact reformer unit for generating hydrogen from gaseous hydrocarbons in the low power range |
NO20041404A NO20041404L (no) | 2001-09-03 | 2004-04-05 | Kompakt reformatorenhet i laveffektomradet for produksjon av hydrogen fra hydrokarbongasser. |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10142999.1 | 2001-09-03 | ||
DE10142999A DE10142999B4 (de) | 2001-09-03 | 2001-09-03 | Hocheffiziente, kompakte Reformereinheit zur Wasserstofferzeugung aus gasförmigen Kohlenwasserstoffen im kleinen Leistungsbereich |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2003024867A1 true WO2003024867A1 (de) | 2003-03-27 |
Family
ID=7697467
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/DE2002/003064 WO2003024867A1 (de) | 2001-09-03 | 2002-08-22 | Kompakte reformereinheit zur wasserstofferzeugung aus gasförmigen kohlenwasserstoffen im kleinen leistungsbereich |
Country Status (12)
Country | Link |
---|---|
US (1) | US7803202B2 (de) |
EP (1) | EP1425244B1 (de) |
JP (1) | JP4504016B2 (de) |
KR (1) | KR100848047B1 (de) |
AT (1) | ATE359232T1 (de) |
CA (1) | CA2459429C (de) |
DE (2) | DE10142999B4 (de) |
DK (1) | DK1425244T3 (de) |
ES (1) | ES2284923T3 (de) |
NO (1) | NO20041404L (de) |
PT (1) | PT1425244E (de) |
WO (1) | WO2003024867A1 (de) |
Cited By (5)
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WO2008146051A1 (en) * | 2007-05-25 | 2008-12-04 | Helbio S.A. Hydrogen And Energy Production Systems | H i g h ly h eat i nt e g rat e d f u e l p ro c e s s o r f o r h y d ro g e n p ro d u ct i o n |
JP2008546628A (ja) * | 2005-06-28 | 2008-12-25 | ハルドール・トプサー・アクチエゼルスカベット | 小型改質反応装置 |
JP2008546627A (ja) * | 2005-06-28 | 2008-12-25 | ハルドール・トプサー・アクチエゼルスカベット | 小型改質反応装置 |
EP2495214A2 (de) | 2011-03-04 | 2012-09-05 | DBI- Gastechnologisches Institut gGmbH Freiberg | Verfahren und Anordnung zur Dampfreformierung kohlenwasserstoffhaltiger Gase |
CN113998670A (zh) * | 2021-12-27 | 2022-02-01 | 广东蓝玖新能源科技有限公司 | 一种制氢机 |
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DE10348638A1 (de) * | 2003-10-15 | 2005-05-25 | J. Eberspächer GmbH & Co. KG | Verdampferanordnung zur Erzeugung eines in einem Reformer zur Wasserstoffgewinnung zersetzbaren Kohlenwasserstoff/Wasserdampf-Gemisches |
DE10359231A1 (de) * | 2003-12-17 | 2005-07-28 | Webasto Ag | System und Verfahren zur Erzeugung eines Reformats |
PL1570901T3 (pl) * | 2004-03-01 | 2009-01-30 | Haldor Topsoe As | Proces chłodzenia strefy reakcji egzotermicznej i zespołu reaktora |
US8886298B2 (en) | 2004-03-01 | 2014-11-11 | Microsoft Corporation | Recall device |
JP4492534B2 (ja) * | 2005-12-28 | 2010-06-30 | カシオ計算機株式会社 | 反応装置および反応装置の製造方法 |
US7506685B2 (en) * | 2006-03-29 | 2009-03-24 | Pioneer Energy, Inc. | Apparatus and method for extracting petroleum from underground sites using reformed gases |
DE102006019407B4 (de) * | 2006-04-23 | 2009-10-22 | Zentrum für Brennstoffzellen-Technik GmbH | Temperaturgeführter Reaktor zur Kohlenmonoxidreinigung |
US8323365B2 (en) * | 2007-05-22 | 2012-12-04 | Praxair Technology, Inc. | Dual mode reactor SMR integration |
DE102008020407A1 (de) | 2007-11-03 | 2009-05-07 | Riesaer Brennstoffzellentechnik Gmbh | Apparatur zur effizienten Erzeugung von Wasserstoff aus kohlenwasserstoffhaltigen Gasen mittels Dampfreformierung |
DE202008003989U1 (de) | 2007-11-03 | 2008-06-26 | Riesaer Brennstoffzellentechnik Gmbh | Apparatur zur effizienten Erzeugung von Wasserstoff aus kohlenwasserstoffhaltigen Gasen mittels Dampfreformierung |
KR100968541B1 (ko) * | 2008-07-09 | 2010-07-08 | 지에스퓨얼셀 주식회사 | 연료전지시스템의 연료변환장치 |
US9227844B2 (en) * | 2010-01-19 | 2016-01-05 | Haldor Topsoe A/S | Heat exchange reformer with double-tubes for reforming hydrocarbons |
FR2969593B1 (fr) * | 2010-12-22 | 2014-08-29 | IFP Energies Nouvelles | Amelioration d'un procede de production d'hydrogene integre thermiquement par reformage d'une charge hydrocarbonee |
ES2743707T3 (es) * | 2012-06-14 | 2020-02-20 | Nuvera Fuel Cells Llc | Reformador con vapor |
KR101898788B1 (ko) * | 2016-12-30 | 2018-09-13 | 주식회사 두산 | 연료처리장치 |
US10651487B2 (en) * | 2017-11-20 | 2020-05-12 | Industrial Technology Research Institute | Modular apparatus of fuel cell system |
US10787363B2 (en) * | 2018-12-27 | 2020-09-29 | Automotive Research & Testing Center | Hydrogen producing apparatus with emulsifier |
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- 2001-09-03 DE DE10142999A patent/DE10142999B4/de not_active Expired - Fee Related
-
2002
- 2002-08-22 PT PT02769879T patent/PT1425244E/pt unknown
- 2002-08-22 KR KR1020047003161A patent/KR100848047B1/ko not_active IP Right Cessation
- 2002-08-22 ES ES02769879T patent/ES2284923T3/es not_active Expired - Lifetime
- 2002-08-22 EP EP02769879A patent/EP1425244B1/de not_active Expired - Lifetime
- 2002-08-22 AT AT02769879T patent/ATE359232T1/de active
- 2002-08-22 CA CA2459429A patent/CA2459429C/en not_active Expired - Fee Related
- 2002-08-22 US US10/488,439 patent/US7803202B2/en not_active Expired - Fee Related
- 2002-08-22 DE DE50209935T patent/DE50209935D1/de not_active Expired - Lifetime
- 2002-08-22 WO PCT/DE2002/003064 patent/WO2003024867A1/de active Search and Examination
- 2002-08-22 DK DK02769879T patent/DK1425244T3/da active
- 2002-08-22 JP JP2003528722A patent/JP4504016B2/ja not_active Expired - Fee Related
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US6162267A (en) * | 1998-12-11 | 2000-12-19 | Uop Llc | Process for the generation of pure hydrogen for use with fuel cells |
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JP2008546628A (ja) * | 2005-06-28 | 2008-12-25 | ハルドール・トプサー・アクチエゼルスカベット | 小型改質反応装置 |
JP2008546627A (ja) * | 2005-06-28 | 2008-12-25 | ハルドール・トプサー・アクチエゼルスカベット | 小型改質反応装置 |
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DE102011013026A1 (de) | 2011-03-04 | 2012-09-06 | Dbi - Gastechnologisches Institut Ggmbh Freiberg | Verfahren und Anordnung zur Dampfreformierung kohlenwasserstoffhaltiger Gase |
CN113998670A (zh) * | 2021-12-27 | 2022-02-01 | 广东蓝玖新能源科技有限公司 | 一种制氢机 |
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Also Published As
Publication number | Publication date |
---|---|
KR20040058180A (ko) | 2004-07-03 |
CA2459429C (en) | 2010-10-19 |
DE10142999A1 (de) | 2003-03-27 |
NO20041404L (no) | 2004-04-05 |
EP1425244B1 (de) | 2007-04-11 |
KR100848047B1 (ko) | 2008-07-23 |
DK1425244T3 (da) | 2007-08-27 |
ES2284923T3 (es) | 2007-11-16 |
JP2005525984A (ja) | 2005-09-02 |
US20060188434A1 (en) | 2006-08-24 |
ATE359232T1 (de) | 2007-05-15 |
PT1425244E (pt) | 2007-07-17 |
CA2459429A1 (en) | 2003-03-27 |
JP4504016B2 (ja) | 2010-07-14 |
EP1425244A1 (de) | 2004-06-09 |
DE50209935D1 (de) | 2007-05-24 |
DE10142999B4 (de) | 2006-07-06 |
US7803202B2 (en) | 2010-09-28 |
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