EP1934135A1 - Systeme reformeur et procede de reformage - Google Patents

Systeme reformeur et procede de reformage

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Publication number
EP1934135A1
EP1934135A1 EP06806190A EP06806190A EP1934135A1 EP 1934135 A1 EP1934135 A1 EP 1934135A1 EP 06806190 A EP06806190 A EP 06806190A EP 06806190 A EP06806190 A EP 06806190A EP 1934135 A1 EP1934135 A1 EP 1934135A1
Authority
EP
European Patent Office
Prior art keywords
adsorber
temperature
reformate gas
hydrocarbons
reformer
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Withdrawn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
EP06806190A
Other languages
German (de)
English (en)
Inventor
Jürgen Ringler
Christian Liebl
Michael Preis
Jochem Huber
John Kirwan
Jean Botti
James Grieve
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.)
Bayerische Motoren Werke AG
Delphi Technologies Inc
Original Assignee
Bayerische Motoren Werke AG
Delphi Technologies Inc
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 Bayerische Motoren Werke AG, Delphi Technologies Inc filed Critical Bayerische Motoren Werke AG
Publication of EP1934135A1 publication Critical patent/EP1934135A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0454—Controlling adsorption
    • 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
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/01—Engine exhaust gases
    • B01D2258/012—Diesel engines and lean burn gasoline engines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/01—Engine exhaust gases
    • B01D2258/014—Stoichiometric gasoline engines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/01—Engine exhaust gases
    • B01D2258/016—Methanol engines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0208—Other waste gases from fuel cells
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40001—Methods relating to additional, e.g. intermediate, treatment of process gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/45—Gas separation or purification devices adapted for specific applications
    • B01D2259/4566—Gas separation or purification devices adapted for specific applications for use in transportation means
    • 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
    • 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
    • C01B2203/042—Purification by adsorption on solids
    • 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
    • C01B2203/048—Composition of the impurity the impurity being an organic compound
    • 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
    • C01B2203/1604—Starting up the process

Definitions

  • the invention relates to a reformer system with a reformer which is designed to convert a hydrocarbon-containing fuel into a hydrogen-gas-rich reformate gas which can be taken off at an outlet of the reformer.
  • the invention further relates to a vehicle with such a reformer system.
  • the invention relates to a method for reforming a hydrocarbon-containing fuel with a conversion of the hydrocarbon-containing fuel into a hydrogen-rich reformate gas by means of a reforming process.
  • Reformersystems are generally used in motor vehicles to produce a hydrogen-rich synthesis gas or reformate gas consisting of hydrogen (H 2 ), carbon monoxide (CO) and inert gas (N 2 , CO 2 , H 2 O) from liquid or gaseous hydrocarbon-containing fuels.
  • H 2 hydrogen
  • CO carbon monoxide
  • N 2 , CO 2 , H 2 O inert gas
  • different reforming methods including partial oxidation, steam reforming, CO 2 - reforming and cracking or combinations thereof (eg autothermal reforming) are known.
  • To increase the hydrogen yield may be followed by a so-called shift reaction.
  • the currently known uses and uses of a reformate gas in a motor vehicle include the operation of a fuel cell, the supply to an internal combustion engine to minimize cold start / warm-up and raw emissions of the same internal combustion engine, and the aftertreatment of exhaust gases from the internal combustion engine.
  • a temperature outside an operating window of a catalyst used in the reformer can lead to a limitation of desired reaction sequences and / or an increased occurrence of undesired side reactions. This tends to cause higher pollutant emissions, including HC emissions.
  • the increased HC emissions of the reformer, especially in the starting phase, have a negative effect on the further use of the reformate gas.
  • the HC emissions can lead to damage to the fuel cell. If the reformate gas is used for starting and / or further operation of an internal combustion engine, high proportions of hydrocarbon in the reformate gas lead to an increase in the emissions of the internal combustion engine.
  • the invention has for its object to provide a reformer system of the type mentioned and a Reformier ⁇ ngs vide of the aforementioned type, whereby a reformate gas can be generated in a stable reaction process, which can be easily processed by a downstream customer.
  • a reformer system comprising a reformer for reacting a hydrocarbon-containing fuel in a hydrogen-rich reformate gas and a reformer downstream HC adsorber, which is designed to adsorb temperature-dependent in the reformate contained hydrocarbons or previously adsorbed hydrocarbons to desorb the reformate gas, wherein the reformer system is designed to forward the reformate gas after passing through the HC adsorber to a customer, and the time course of the adsorption / desorption of the HC adsorber during an operating phase of the reformer as a function of the in the operating phase occurring Reformatgastemperatur and / or a temperature gradient of the reformate gas occurring in the operating phase is tuned to the time course of the operating behavior of the customer that a substantial desorption of Kohlenwa Hydrogen from the HC adsorber takes place only when the customer is in an operating condition in which the desorbed hydrocarbons are processed by the customer such that the hydrocarbon content of the gas emitted by the customer and / or the function
  • the object is achieved with a method for reforming a hydrocarbon-containing fuel with a conversion of the hydrocarbon-containing fuel into a hydrogen-rich reformate gas by means of a reforming process, a temperature-dependent adsorption in the Hydrocarbon reformate contained in a HC adsorber or desorb previously adsorbed hydrocarbons to the reformate, and forwarding the reformate gas after passing through the HC adsorber to a customer, the time course of the adsorption / desorption of the HC adsorber during an operating phase the reformer in response to the occurring in the operating phase reformate gas temperature and / or occurring in the operating phase temperature gradient of the reformate gas is tuned to the time course of the operating behavior of the consumer that a substantial desorption of hydrocarbons from the HC adsorber takes place only if the purchaser is in an operating condition in which the desorbed hydrocarbons are processed by the purchaser such that the hydrocarbon portion of the gases discharged by the purchaser and / or the function of the purchaser by the desorbed hydrocarbons is not significantly
  • the quality of the fuel or the quality of the air / fuel mixture need not be considered during operation phase of the reformer, in particular during its start phase become.
  • the conditions of the reforming process can be specifically adapted to the other requirements of the operating phase and thereby kept stable. It is a stable flow of the reaction process allows.
  • the solution according to the invention makes it possible to optimize the reforming method without regard to corresponding marginal conditions owing to the HC emission behavior with regard to rapid starting capability and / or durability.
  • the operating behavior of the consumer is influenced by the reformate gas temperature, the temperature gradient of the reformate gas and / or the concentration of hydrocarbons. Due to the dependence of the adsorption / desorption behavior of the HC adsorber on the reformate gas temperature, the influence of the time-dependent change in the reformate gas temperature on the Operating behavior of the customer considered accordingly.
  • the HC adsorber according to the present invention may have a high adsorption capability influenced by a low reformate gas temperature in the operation phase, such as at the start of the reforming process in which a large amount of hydrocarbons is generated. In this phase, the reformate gas reaching the consumer is essentially hydrocarbon-free or contains only a small proportion of hydrocarbon.
  • the customer is still "cold" in this phase and would be hampered in its function by a high proportion of hydrocarbons or the gases emitted by the customer would be characterized by high emissions.
  • the reformer process progresses, such as in the period following the startup phase, the reformate gas temperature now rises, causing the HC adsorber to absorb fewer hydrocarbons.
  • the downstream consumer is less hindered in its function by the reformate gas temperature, even at elevated hydrocarbon content in the reformate gas or is able to process hydrocarbons such that the gas ejected from the customer are less contaminated by hydrocarbons. If the temperature of the reformate gas reaches a certain threshold value, then the hydrocarbons previously taken up by the HC adsorber are released from it again.
  • the consumer is in a condition to process a large amount of hydrocarbons in the reformate gas without significantly affecting its function or producing undesirable emissions.
  • the reformate gas produced by the reformer can thus be processed without problems, ie, without impairing the function of the consumer or without producing undesired pollutants, to an excessive extent.
  • the reformate gas is supplied to an exhaust aftertreatment system of an internal combustion engine which functions as a consumer, substantial desorption of hydrocarbons from the HC adsorber should take place only when, for example, a catalyst provided in the exhaust aftertreatment system has reached or exceeded its light-off temperature.
  • the embodiment according to the invention thus enables a reduction in the HC Adsorber hydrocarbons without corresponding pollution of the environment with hydrocarbon emissions.
  • the operating phase of the reformer comprises a start phase, during which the time profile of the adsorption / desorption of the HC adsorber in response to the rising in the start phase Reformatgastemperatur and / or occurring in the startup temperature gradient of the reformate gas on the time course of Tuning behavior of the customer is tuned that a substantial desorption of hydrocarbons from the HC adsorber takes place only when the customer is in an operating condition in which the desorbed hydrocarbons are processed by the customer such that the hydrocarbon content of the gases emitted by the customer and / or the function of the customer is not significantly affected by the desorbed hydrocarbons.
  • the customer comprises an exhaust aftertreatment system, an internal combustion engine and / or a fuel cell.
  • an internal combustion engine can be provided, which is supplied to minimize its cold start, warm-up and raw emissions, the hydrogen gas-rich reformate gas.
  • a substantial desorption of hydrocarbons takes place only when the combustion conditions in the internal combustion engine have stabilized such that the additional hydrocarbon content of the reformate gas has no negative effects on the HC emissions of the internal combustion engine.
  • the tuning of the adsorption / desorption behavior of the HC adsorber in dependence on the reformate gas temperature takes place by suitable selection of the material of the HC adsorber and / or by suitable positioning of the HC adsorber.
  • suitable positioning of the HC adsorber in closer proximity or further away from the Reformer can be adjusted by the natural cooling of the reformate gas along the route the reformate gas temperature to the adsorption / desorption of the HC adsorber accordingly.
  • the hydrocarbon-containing fuel convertible by the reformer is liquid, and contains in particular gasoline, diesel and / or alcohols. Adsorption of hydrocarbons following the reforming process proves to be particularly advantageous in a reformate gas produced from liquid fuel. This is due to the fact that the emission behavior during the reformer start even further deteriorates when using liquid fuel, since at low temperature of the occurring before the reforming reaction between a liquid medium and air homogenization process is difficult.
  • the HC adsorber In order to extract hydrocarbons from the reformate gas in a particularly effective manner, it is expedient for the HC adsorber to have activated carbon and / or a substance having a pore structure which functions as a molecular sieve, in particular zeolite. It is particularly advantageous if this substance is applied to monolithic carriers and additionally catalytically activated as needed.
  • the HC adsorber can be advantageously based on adsorber materials and methods that are also used in minimizing HC emissions from the fuel supply system or engine emissions during startup and warm-up of an internal combustion engine.
  • the function of the HC adsorber is tuned to the reformate gas temperature that at a reverse temperature of the reformate gas, the adsorption of the hydrocarbons from the reformate gas is compensated by a desorption of the adsorbed hydrocarbons to the reformate gas, and below the reversal temperature, the adsorption and above the Reverse temperature, the desorption predominates.
  • the inversion temperature for a typical reformate gas is not a fixed value but represents a region in which adsorption still exists for certain species but is desorb for other species. This is due to the fact that there is an individual inversion temperature for each HC species.
  • the selection and design of the adsorber material of the HC adsorber can be used to optimize the adsorption and desorption behavior quasi-selectively via the temperature to specific hydrocarbon species.
  • the value of the reversal temperature depends on physical boundary conditions, such as pressure of the reformate gas, degree of saturation of the HC adsorber and / or water content of the reformate gas, as well as the type of adsorbed hydrocarbon species and selection of the adsorber.
  • the inventive temperature-dependent reversal behavior of the hydrocarbon adsorption allows the reformer system to be operated as follows.
  • the HC adsorber has a large capacity for the hydrocarbon molecules due to the relatively low reformate gas temperature.
  • the reforming process stabilizes, with the result that the hydrocarbon emissions from the reformer go back to an uncritical level.
  • the reformate gas temperature is above the reversal temperature of the HC adsorber, whereby a desorption of the adsorbed during the start and run-up of the reformer hydrocarbons. This desorption is expediently carried out with a rate which is acceptable for the purchaser of the reformate gas.
  • the total hydrocarbon concentration in the reformate gas supplied to the consumer can still be kept within an acceptable range, even with some increase in hydrocarbon content by desorption from the HC adsorber.
  • the HC adsorber deflates so far that it is sufficiently receptive again in the case of a renewed starting process of the reformer.
  • the reversal temperature of the HC adsorber is smaller than the equilibrium temperature of the reformate gas and / or the adsorption capacity of the HC adsorber for hydrocarbons, in particular for the hydrocarbon species contained in the reformate gas at a relatively low temperature to the equilibrium temperature, in particular at a temperature of at most 100 0 C, has a maximum.
  • An HC adsorber designed in such a way as to be of its type and nature permits optimum hydrocarbon reduction of the reformate gas during the start-up phase of the reformer in which the hydrocarbon content in the reformate gas is highest.
  • the HC adsorber is designed such that hydrocarbons adsorbed above a discharge temperature at a temperature of the reformate gas desorb the HC adsorber instantaneously and completely to the reformate gas.
  • the hydrocarbons of the HC adsorber should desorb in the shortest possible time to as 100% as possible in a relevant temperature range above the emptying temperature.
  • the emptying temperature may suitably be above the reversal temperature.
  • the exact value of the emptying temperature is, as well as the value of the reversal temperature of physical boundary conditions, such as pressure of the reformate, saturation of the HC adsorber and / or water content of the reformate gas and type of adsorbed hydrocarbon species and selection of the adsorber dependent.
  • the HC adsorber is designed such that at a temperature of the reformate gas below the discharge temperature previously adsorbed hydrocarbons of the HC adsorber with a relative to the desorption above the drain temperature low rate to the reformate gas desorb.
  • the HC adsorber has this relatively low desorption rate in a temperature range between the inversion temperature and the discharge temperature.
  • the desorption rate of the HC adsorber in the temperature range between the reversal temperature and the emptying temperature is lower than the adsorption rate of the HC adsorber at a temperature below the reversal temperature.
  • the reformer system has a heat exchanger connected downstream of the reformer, by means of which the temperature of the reformate gas changeable, in particular reducible.
  • the heat exchanger upstream of the HC adsorber and / or the HC adsorber is integrated into the heat exchanger, in particular hydrocarbon adsorbing material of the HC adsorber is contained in walls of the heat exchanger.
  • the heat exchanger and the HC adsorber are two separate devices, wherein the reformate leaving the reformer first passes through the heat exchanger and then with a matched to the adsorption or desorption of the HC adsorber temperature through the HC Adsorber is performed.
  • the type and nature of the material of the HC adsorber is chosen so that the temperature window of the HC adsorber, takes place in the desorption of hydrocarbons to the reformate gas, so that it is self-adjusting or heat exchange adjustable Reformatgastemperaturen contains.
  • the hydrocarbon exchange with the HC adsorber proceeds simultaneously with the temperature change of the reformate gas by means of the heat exchanger.
  • This alternative is particularly space-saving.
  • a hydrocarbon adsorbing material for integration into the walls of the heat exchanger is in particular a material with zeolitic structures.
  • the arrangement of the HC adsorber is expediently carried out after the reformer system or after the heat exchanger at a position at which it is best possible to set the optimum adsorption or desorption temperature window on the HC adsorber for the overall process.
  • the heat exchanger is designed to adjust the temperature of the reformate gas to a suitable, in particular optimum temperature for adsorption or desorption of the hydrocarbons by the HC adsorber.
  • the heat output of the reformate gas in the heat exchanger is controlled so that the adsorption and desorption of hydrocarbons at and from the HC adsorber in a respect of Adsorptions- or desorption efficiency optimal temperature window occurs.
  • the reformer system according to the invention has extraction means by means of which at least part of the reformate gas can be branched off from the reformate gas stream before entry into the HC adsorber between the outlet of the reformer and the HC adsorber, in particular before and / or after the heat exchanger, and a customer, in particular an exhaust aftertreatment system can be fed.
  • Fig. 2 is a greatly simplified illustration of the reformer system of FIG. 1 with a heat exchanger.
  • a reformer system according to the invention is shown schematically.
  • This includes a fuel line 10 in which liquid fuel 12, such as gasoline or diesel, may be supplied to a reformer 14.
  • liquid fuel 12 such as gasoline or diesel
  • the liquid fuel first passes into a mixture forming zone in which it is mixed by evaporation with an air supplied from the outside. Then, the air / fuel mixture is reacted in a reaction zone of the reformer 14 by means of a reforming process in a hydrogen-rich reformate gas.
  • a reforming process partial oxidation, steam reforming, CO 2 reforming, cracking or combinations thereof, such as autothermal reforming, in question.
  • To increase the hydrogen yield may be followed by a so-called shift reaction.
  • the reforming processes take place without catalyst at about 1500 ° C.
  • the reforming temperature can be lowered by using a catalyst to about 800 to 1000 ° C.
  • the reformate gas or synthesis gas produced by the reforming process exits at the outlet 15 of the reformer 14 and consists of hydrogen (H 2 ), carbon monoxide (CO) and inert gas (N 2 , CO 2 , H 2 O).
  • the reformate gas 18 is then fed by means of a gas line 16 to a HC adsorber 20.
  • the HC adsorber 20 may have an activated carbon filter or also as molecular sieves functioning pore structures, such as zeolites, which are applied to monolithic carrier substances and can be additionally activated catalytically, if necessary.
  • the HC adsorber 20 removes the reformate gas 18 by adsorption contained therein hydrocarbons. However, this adsorption process takes place only for temperatures of the reformate gas below a certain inversion temperature. If the reformate gas 18 has a higher temperature, desorption of hydrocarbon molecules deposited in the HC adsorber 20 by means of the preceding adsorption process takes place on the reformate gas 18.
  • the type and nature of the hydrocarbon adsorbing material is designed so that during the start phase of the Reformers 14 is given a maximum adsorption capacity of the HC adsorber for the reformate gas 18 resulting temperatures. At reformate gas temperatures at which the reformer 14 is already in a stable operating condition, the reformate gas 18 produced hardly contains any more hydrocarbon emissions. At these reformate gas temperatures, the HC adsorber 20 is in the operating mode in which the hydrocarbons are again desorbed very slowly.
  • the treated reformate gas 24 is supplied to a customer, such as an exhaust aftertreatment system 26, an internal combustion engine 28, and / or a fuel cell 30.
  • untreated reformate gas 18 can be removed from the gas line between the reformer 14 and the HC adsorber 20 by means of a branching element 32 and supplied to the exhaust aftertreatment system 26 via a further gas line 34.
  • a heat exchanger or heat exchanger 36 is connected between the reformer 14 and the HC adsorber 20. This serves to either increase or decrease the temperature of the untreated reformate gas 18 in order to optimize the adsorption or desorption yield in the downstream HC adsorber 20.
  • the temperature of the entering into the HC adsorber 20 reformate gas 18 can be adjusted during the start-up phase of the reformer 14 thereon, an optimal adsorption of it Hydrocarbons contained in the HC adsorber 20 to cause.
  • the consumer such as the internal combustion engine 28, is still “cold” and would be hampered in its function by a high proportion of hydrocarbons or the gases expelled from the internal combustion engine 28 would be characterized by high emissions which causes the HC adsorber 20 to absorb fewer hydrocarbons, but the downstream engine 20 is less obstructed in its function by the reformate gas temperature, even at elevated hydrocarbon content in the reformate gas, or is capable of processing hydrocarbons such that When the reformate gas temperature reaches a certain threshold value, the hydrocarbons previously taken up by the HC adsorber 20 are released therefrom again, at this reformate gas temperature
  • the internal combustion engine 28 in a state in which it can process a large amount of hydrocarbons in the reformate gas, without being significantly impaired in its function or without producing unwanted emissions.
  • the temperature of the reformate gas 18 can also be adjusted to a desired desorption rate of hydrocarbons from the HC adsorber 20.
  • a branch element 32 or 32 'for supplying untreated reformate gas 18 to the exhaust aftertreatment system 26 is provided both before and after the heat exchanger 36. Upon removal of the reformate gas 18 even before the heat exchanger 36 by means of the branching element 32, additional heat can be introduced into the exhaust gas of the exhaust gas treatment system 26.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

La présente invention concerne un système reformeur comprenant un reformeur (14) conçu pour transformer un carburant contenant des hydrocarbures (12) en un gaz de reformage riche en hydrogène gazeux (18). Ce système reformeur présente un adsorbeur de HC (20) qui est connecté en aval du reformeur et qui est conçu pour adsorber les hydrocarbures contenus dans le gaz de reformage en fonction de la température ou pour désorber sur le gaz de reformage des hydrocarbures préalablement adsorbés. Le système reformeur est conçu pour transmettre le gaz de reformage (18) à un récepteur (26, 28, 30) après passage par l'adsorbeur de HC (20). La variation dans le temps du rapport adsorption/désorption de l'adsorbeur de HC (20) est adaptée à la variation dans le temps de la performance de fonctionnement du récepteur (26, 28, 30) au cours d'une phase de fonctionnement du reformeur, en fonction de la température du gaz de reformage apparaissant dans la phase de fonctionnement et/ou d'un gradient de température du gaz de reformage apparaissant dans la phase de fonctionnement, de telle manière qu'une désorption importante d'hydrocarbures à partir de l'adsorbeur de HC (20) n'a lieu que lorsque le récepteur (26, 28, 30) se trouve dans un état de fonctionnement dans lequel les hydrocarbures désorbés sont traités par le récepteur (26, 28, 30) de façon que la fraction d'hydrocarbures des gaz produits par le récepteur (26, 28, 30) et/ou le fonctionnement du récepteur (26, 28, 30) ne soient pas influencés de manière sensible par les hydrocarbures désorbés.
EP06806190A 2005-10-13 2006-10-11 Systeme reformeur et procede de reformage Withdrawn EP1934135A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US11/248,162 US20070086934A1 (en) 2005-10-13 2005-10-13 Reformer system and method reforming
PCT/EP2006/009826 WO2007042278A1 (fr) 2005-10-13 2006-10-11 Systeme reformeur et procede de reformage

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Families Citing this family (5)

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Publication number Priority date Publication date Assignee Title
US8539914B2 (en) * 2010-04-08 2013-09-24 Ford Global Technologies, Llc Method for operating an engine with a fuel reformer
US9955986B2 (en) 2015-10-30 2018-05-01 Auris Surgical Robotics, Inc. Basket apparatus
US10639108B2 (en) 2015-10-30 2020-05-05 Auris Health, Inc. Process for percutaneous operations
US9949749B2 (en) 2015-10-30 2018-04-24 Auris Surgical Robotics, Inc. Object capture with a basket
JP2023508718A (ja) 2019-12-31 2023-03-03 オーリス ヘルス インコーポレイテッド 高度バスケット駆動モード

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3676563A (en) * 1970-04-06 1972-07-11 Airco Inc Hyperbaric breathing mixture
ES2640910T3 (es) * 2000-10-27 2017-11-07 Air Products And Chemicals, Inc. Sistemas y procesos para proporcionar hidrógeno a células de combustible
US6746515B2 (en) * 2001-04-30 2004-06-08 Battelle Memorial Institute Method and apparatus for thermal swing adsorption and thermally-enhanced pressure swing adsorption
US6728602B2 (en) * 2002-03-15 2004-04-27 Delphi Technologies, Inc. Control system for an electric heater
US6832473B2 (en) * 2002-11-21 2004-12-21 Delphi Technologies, Inc. Method and system for regenerating NOx adsorbers and/or particulate filters
US20040253493A1 (en) * 2003-06-11 2004-12-16 Nissan Technical Center N. A. Inc. Reformate purifying system for fuel processing systems
WO2005007567A1 (fr) * 2003-06-20 2005-01-27 Detroit Edison Company Dispositif et procede destines au reformage d'un gaz cov

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2007042278A1 *

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WO2007042278A1 (fr) 2007-04-19

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