GB2381533A - Supercritical reformer - Google Patents

Supercritical reformer Download PDF

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Publication number
GB2381533A
GB2381533A GB0217179A GB0217179A GB2381533A GB 2381533 A GB2381533 A GB 2381533A GB 0217179 A GB0217179 A GB 0217179A GB 0217179 A GB0217179 A GB 0217179A GB 2381533 A GB2381533 A GB 2381533A
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United Kingdom
Prior art keywords
reformer
reformer unit
unit according
fluids
reformate
Prior art date
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GB0217179A
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GB0217179D0 (en
Inventor
Norbert Breuer
Christian Schiller
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Robert Bosch GmbH
Original Assignee
Robert Bosch GmbH
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Publication date
Application filed by Robert Bosch GmbH filed Critical Robert Bosch GmbH
Publication of GB0217179D0 publication Critical patent/GB0217179D0/en
Publication of GB2381533A publication Critical patent/GB2381533A/en
Withdrawn legal-status Critical Current

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    • 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
    • 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
    • B01J19/2475—Membrane 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
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/008—Processes carried out under supercritical conditions
    • 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
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • B01J8/009—Membranes, e.g. feeding or removing reactants or products to or from the catalyst bed through a membrane
    • 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
    • B01J8/0278—Feeding reactive fluids
    • 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
    • B01J8/0285—Heating or cooling the reactor
    • 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
    • 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
    • B01J2208/00539—Pressure
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00004—Scale aspects
    • B01J2219/00006—Large-scale industrial plants
    • 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
    • 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
    • C01B2203/0405—Purification by membrane separation
    • 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
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/066—Integration with other chemical processes with fuel cells
    • 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
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1217—Alcohols
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1276—Mixing of different feed components
    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
    • 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
    • C01B2203/16—Controlling the process
    • C01B2203/169—Controlling the feed
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Fuel Cell (AREA)

Abstract

A reformer unit for producing a hydrogen-rich reformate (R) from at least one second fluid (B), in particular water and/or oxygen, which transforms a hydrocarbon-rich first fluid (A), said reformer unit having a reformer device (D), is proposed which ensures a particularly compact embodiment and at the same time reduces processing costs. This is achieved according to the invention in that at least one of the fluids (A, B) takes the form of a supercritical fluid (A, B). The hydrogen produced may be used in a fuel cell.

Description

238 1 533
Reformer unit for producing a reformats The invention relates to a reformer unit for producing a hydro en-rich reformate according to the precharacterising clause of claim I. Prior art
For many years, hydrocarbon reforming has been performed principally using partial oxidation processes and steam reforming to produce a hydrogen-rich gas stream comprising hydrocarbons. Gas purification stages are provided with these processes, to reduce the carbon monoxide content in the gas stream to approximately 100 ppm for example for a low temperature fuel cell. In general, a plurality of processing stages are provided therefor, so entailing not inconsiderable processing and structural expenditure. This brings with it relatively high costs for process development and manufacture and comparatively high maintenance requirements for the entire installation. Object and advantages of the invention In contrast, the object of the invention is to propose a reformer unit for producing a hydrogen-rich reformate from at least one second fluid which transforms' in particular oxidises, a hydrocarbon-rich first fluid which reformer unit ensures a particularly compact embodiment and at the same time reduces the processing costs.
This object is achieved, on the basis of prior art of the above-mentioned type, by the
characterising features of claim 1.
Advantageous embodiments and further developments of the invention are possible as a result of the measures mentioned in the subclaims.
Accordingly, a reformer unit according to the invention is distinguished in that at least one of the fluids takes the form of a supercritical fluid. A supercritical fluid is understood to mean a fluid which is above its critical temperature and its critical pressure. In contrast to reformers according to the prior art, according to the invention an
increase in operating temperature or in operating pressure does not have a disadvantageous effect on reforming. The reformer unit according to the invention with a supercritical fluid combines the advantages of the gaseous and liquid phases of the fluid, wherein it is no longer possible to distinguish between the liquid and the gaseous phase.
For example, in the case of a supercritical fluid, the density, polarity and dielectric and/or dissociation constant of the fluids change advantageously Advantageous reaction paths are thereby obtained for fluid reforming and the reaction rate is virtually unlimited by mass transfer.
The critical parameters for pressure and temperature of a number of organic compounds, including water, are listed below by way of example: Compound Pressure [barl Temperature [K] Methanol 80.9 512.6 Ethanol 61.4 513.9 Naphtha 24.9 568.9 Water 221.3 647.1 When using supercutical naphtha and water, a homogeneous mixture or phase is thereby obtained, such that, in contrast to the corresponding heterogeneous prior art
mixture, it is not generally necessary to provide any complex mixing and/or atomisation devices.
,. A.__ I Illles IaIBi e; 1 11 11 11 j11 1111111 11 1 'B11111 111 11111i
For the above-mentioned reasons, a reformer unit according to the invention may be substantially more compact or lighter in construction than the prior art inter alla with
relatively high power densities and be obtained at markedly lower cost.
To achieve the operating conditions according to the invention, it is preferable to provide at least one heating device for heating at least one of the fluids to above the critical temperature and advantageously at least one pressure generating device for pressurising at least one of the fluids to above critical pressure. Two heating devices and/or two pressure generating devices are optionally provided, wherein, in this variant of the invention, the two fluids are each heated and/or pressurised separately and then combined or introduced into the reformer device.
In particular to reduce structural complexity, it is preferable to use only one heating device or one pressure generating device. The reformer device preferably contains at least the heating device. Alternatively or in combination therewith, the heating device is arranged upstream of the reformer device in the direction of flow of the fluids, such that preheating or heating of the fluid(s) is optionally made possible, these then being introduced into the reformer device.
In a preferred variant of the invention, the pressure generating unit is arranged upstream of the reformer device in the flow direction, such that the fluid or fluids may be introduced into the reformer device at supercritical pressure. A high-pressure pump or the like may advantageously be used to generate the supercritical pressure.
In an advantageous embodiment of the invention, at least one mixing device is provided for combining the fluids. This mixing device may be either incorporated into the reformer device or arranged upstream of the reformer device in the flow direction of the fluids, in particular upstream of the pressure generating unit.
In the variant of the invention in particular in which the mixing device is arranged upstream of the pressure generating unit in the flow direction of the fluids.
advantageous low pressure mixing is possible. In contrast, in the case of high pressure mixing of the fluids, at least two pressure generating units are necessary.
At least one metering element is preferably provided for metering at least one of the fluids. By means of this measure, an advantageous ratio of the quantities of fluid to be supphed to the reformer device is achieved. In addinon, the fluid streams to be supplied may be conformed to reforming or to downstream consumers and/or storage units by means of an advantageous closed and/or open loop control unit.
In a particular variant of the invention, at least one purification device is provided for extensive purification of the reformate of undesired material components.
Purification of the reformate is preferably performed in accordance with any reformate consumers or converters which may follow downstream.
For example, if the reformer unit is used in fuel cell installations, carbon monoxide components in particular in the reformate may damage a downstream fuel cell unit, such that, for this instance of application in particular, the carbon monoxide components are as far as possible removed from the reformate or transformed.
The purification device advantageously comprises at least one selectively permeable membrane for separating the material components from the reprobate. In general, purification of the reformats by means of appropriate membranes is effected at comparatively high pressures, such that, in this variant of the invention, the supercritical or critical pressure of the reformer device may advantageously be used to operate the membrane. The pressure of the material stream to be supplied to the fuel cell unit or the like may preferably be advantageously reduced or confonned to the corresponding operating conditions by means of the membrane.
One or more "shift" stages and/or fine purification according to the prior art may
optionally also be used as the purification device. Using a purification device with an .! Be_ 114141 _ 1 I 111111 _ I HI F I all al ICII 1111: 1181: 111111 1 IIE11- 1, 181111 1
appropriate membrane advantageously reduces the complexity and the volume of the entire unit substantially.
Furthermore, in general the reformats is purified in such a way, by using a hydrogen-
permeable membrane, e.g. made at least in part from palladium or the like, that the purified reformats may be supplied directly or optionally via a storage unit or the like to a fuel cell unit without further, additional purification.
In a particular further development of the invention, the purification device is arranged as a separate purification device downstream of the reformer device in the direction of flow of the fluids, so making it comparatively easily accessible or replaceable, among other things for repair and/or maintenance measures.
The reformer device advantageously contains the purification device. A particularly compact reformer unit may be achieved by means of this measure, such that this variant of the invention is designed for use in particular in applications with a comparatively small amount of available space.
At least one pressure recovery unit is preferably arranged downstream of the reformer device in the direction of flow, to recover the pressure from the material components and/or the reformats. This advantageously allows at least partial recovery of the energy used to generate the corresponding fluid pressure. For example, the energy may be recovered from the compressed product gases by means of an expander, a turbine or the like, whereby, in particular, the efficiency of the overall system is additionally increased.
At least one recirculation line is advantageously provided for at least partial recirculation of the material components and/or the reforrnate to the reformer device By means of an appropriate recirculation line, nonreformed components of the stream which has already flowed through the reformer device may optionally flow through the reformer device a,ain and thereby be reformed. This further improves
reforming of the starting materials used, such that the efficiency of the overall system is increased.
In general, the reformer unit according to the invention may be operated endo-, exo-
or autotherrnically. The reforming energy balance may be influenced appropriately in particular by varying the second fluid. For example, to this end, water, air or oxygen may be introduced as the second fluid separately or optionally at the same time into the reformer device at a predetermined ratio in gaseous form or optionally indirectly by combination with precursors such as hydrogen peroxide or the like.
In contrast to the prior art, it is possible in general to do without using catalytically
active material in the reformer device for catalytic reforming of the fluids. In this way, in particular the service life of the reformer unit accordin,, to the invention is increased without a corresponding drop in performance over time. Catalytically active material may optionally also advantageously be used.
Furthermore, the reformer unit according to the invention without catalytically active material is distinctly less sensitive to catalyst poisons such as for example hydrogen sulfide or the like, which is generally present in hydrocarbon-rich fluids such as diesel or naphtha, in addition to other sulfurous compounds. Accordingly, commercially available naphtha or diesel may optionally be used advantageously for the reformer unit according to the invention.
In general, a comparatively compact reformer unit may, according to the invention, optionally take the form of a structural unit. In this way, inter alla the possibilities for use of reformer units according to the invention are increased in comparison to the prior art.
Exemplary embodiment ___',r,__ j,',_e, jj' JO - j ' i1 li,, CB;31:,ll 15,; 1;;lill ll,ll;; ' l - I
An exemplary embodiment of the invention is illustrated in the drawing and is explained in more detail with reference to the single Figure.
Fig 1 is a schematic block diagram of a reformer unit according to the invention The reformer unit comprises two fluid storage vessels 1 and 2 for storing a hydrocarbon-
rich feedstock A and an oxidation agent B. An alcohol such as methanol, ethanol etc. Or naphtha, diesel or the like as well as appropriate mixtures may be used as the feedstock A. The oxidation agent B or an oxygen source may optionally be in aqueous solution.
The ratio between the fluids A and B is so set that on the one hand higher hydrocarbons are oxidatively cracked and on the other hand the hydrogen formed does not undergo undesired secondary reactions with oxygen-containing species.
The two fluids A, B are fed at a temperature Tl and a pressure P1 to a mixer 3 by means of two metering valves 11,]2. The temperature Tl and pressure PI correspond for example to ambient conditions. The mixer 3 may optionally take the form of a commercially available pipe connection or the like.
The two, optionally heterogeneously mixed fluids At B are pressurised to a supercritical pressure P2 by means of a pump C. A reformer D is arranged downstream of the pump C in the direction of flow, which reformer D comprises a heating device not described in any more detail, which heats the fluids A, B or the mixture thereof to a supercritical temperature T2. The two starting materials A, B are reformed in the reformer D under supercritical operating conditions, i.e. in particular transformed into a hydrogen-rich reformate R. The hydrogen-rich reformats R is fed to a purification stage E. The purification stage E comprises a hydrogen-permeable membrane for example, such that two material streams H and S are produced. The material stream H consists, on the other hand,
substantially of hydrogen. The material stream S consists substantially of carbon monoxide, carbon dioxide, non-reformed components of the starting materials, etc. The hydrogen H is supplied for example to a fuel cell unit not described in any more detail. The material stream S is fed for example to an expander F. whereby the compression energy from the compressed product gases may be recovered.
A branch 4 is optionally provided, which allows in particular partial recirculation of the components of the reformate R not converted into hydrogen. These recirculated components are introduced preferably by means of a metering element 5, with which In particular the ratio between the recirculated material stream S and the supplied fluids A, Et may be adjusted.
__.,.,.,._,,.__,i,i,_,. 1 111_1;1 5111 1111 11-IC1 1 111111 1111- 111 111 11 1

Claims (18)

Claims
1 A reformer unit for producing a hydrogen-rich reformate (R) from at least one second fluid (B), in particular water and/or oxygen, which transforms a hydrocarbon-
rich first fluid (A), said reformer unit having a reformer device (D), characterised in that at least one of the fluids (A, B) takes the form of a supercritical fluid (A, B).
2. A reformer unit according to claim 1, characterised in that at least one heating device is provided for heating at least one of the fluids (A, B) to above the critical temperature (T2).
3. A reformer unit according to one of the preceding claims, characterised in that at least one pressure generating device (C) is provided to pressurise at least one of the fluids (A, B) to above the critical pressure (P2).
4. A reformer unit according to one of the preceding claims, characterised in that at least one mixing device (3) is provided for combining the fluids (A, B).
5 A reformer unit according to one of the preceding claims, characterised in that the mixing device (3) is arranged upstream of the pressure generating unit (C) in the direction of flow of the fluids (A, B).
6. A reformer unit according to one of the preceding claims, characterised in that at least one metering element (11, 12) is provided for metering at least one of the fluids (A, B)
7. A reformer unit according to one of the preceding claims, characterised in that at least one purification device (E) is provided extensively to purify the reformate (R) of undesired material components (S)
8 A reformer unit according to one of the preceding claims, charactensed in that the purification device (E) comprises at least one selectively permeable membrane for separating the material components (S) from the reformate (R).
9 A reformer unit according to one of the preceding claims, characterised in that the reformer device (D) comprises the punBcati Mice Aft.
10. A reformer unit according to one of the preceding claims, characterized in that at least one pressure recovery unit (F) is arranged downstream of the reformer device (D) in the direction of flow to recover the pressure (P2) from the material components (S) and/or the reforrnate (R).
11. A reformer unit according to one of the preceding claims, characterized in that at least one recirculation line is provided for at least partial recirculation of the material components (S) and/or the reformate (R) to the reformer device (D).
12. A fuel cell installation with a reformer unit for producing a reformate (R), which is provided as the fuel for a fuel cell unit, characterized in that the reformer unit is constructed in accordance with one of the preceding claims.
13. A waste gas treatment installation with a reformer unit for producing a reformats (R), which is provided as the reducing agent for reducing a waste gas stream from a combustion apparatus, characterized in that the reformer unit is constructed in accordance with one of the preceding claims.
14. A process for producing a hydrogen-rich reformate (R) from at least one second fluid (B), in particular water and/or oxygen, which oxidises a hydrocarbon-
rich first fluid (A), characterized in that a reformer unit according to one of the preceding claims is used.
,__. _ l. l lial I Il_l fall 11 fall I_11111111 1 1_1 L I 11111
15. A process for operating a fuel cell installation, characterized in that the fuel cell installation according to claim 12 is used.
]6. A process for operating a waste gas treatment installation, characterized in that the waste gas treatment installation according to claim 13 is used.
17. A reformer unit substantially as herein described with reference to the accompanying drawings.
18. A process for producing a hydrogen-rich reformate, substantially as herein described with reference to the accompanying drawings.
GB0217179A 2001-07-27 2002-07-24 Supercritical reformer Withdrawn GB2381533A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE10136769A DE10136769A1 (en) 2001-07-27 2001-07-27 Reformer unit for generating a reformate

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GB0217179D0 GB0217179D0 (en) 2002-09-04
GB2381533A true GB2381533A (en) 2003-05-07

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DE (1) DE10136769A1 (en)
FR (1) FR2827852A1 (en)
GB (1) GB2381533A (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2026901A2 (en) * 2006-04-07 2009-02-25 Chart Industries, Inc. Supercritical process, reactor and system for hydrogen production
US7732499B2 (en) 2004-07-09 2010-06-08 Acetex (Cyprus) Limited Preparation of syngas for acetic acid synthesis by partial oxidation of methanol feedstock
ITMI20121537A1 (en) * 2012-09-17 2014-03-18 Maurizio Archetti APPARATUS AND METHOD FOR GASIFICATION OF LIQUID FUEL

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10257255A1 (en) * 2002-12-07 2004-06-24 Daimlerchrysler Ag Fuel cell system for powering automobile propulsion drive incorporating mixing device in anode circuit for mixing liquid fuel with fuel/water mixture
BRPI0614609A2 (en) * 2005-08-03 2016-11-08 Univ Alabama silanes as a hydrogen source
DE102007060512B4 (en) * 2007-12-13 2012-07-12 Eads Deutschland Gmbh Apparatus and method for producing hydrogen gas by dehydrogenating hydrocarbon fuels

Citations (3)

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