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  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
  • B01J2219/00085—Plates; Jackets; Cylinders
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  • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
  • B01J2219/00103—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor in a heat exchanger separate from the reactor
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  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
  • B01J2219/00108—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
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  • B01J2219/00051—Controlling the temperature
  • B01J2219/00139—Controlling the temperature using electromagnetic heating
  • B01J2219/00141—Microwaves
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  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00051—Controlling the temperature
  • B01J2219/00157—Controlling the temperature by means of a burner
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  • C01B2203/02—Processes for making hydrogen or synthesis gas
  • C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
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  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
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  • C01B2203/0405—Purification by membrane separation
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  • C01B2203/0465—Composition of the impurity
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  • 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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  • C01B2203/0805—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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  • C01B2203/1205—Composition of the feed
  • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
  • C01B2203/1235—Hydrocarbons
• • 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
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
  • Y02E60/30—Hydrogen technology
  • Y02E60/32—Hydrogen storage
• • 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
  • Y02P20/10—Process efficiency

Definitions

• the invention relates to a process for the pyrolysis of hydrocarbons or oxygenated fuels (alcohols, ETB, MTB, ...) intended to produce a gas rich in hydrogen and possibly for certain applications of carbon monoxide (CO). It applies, in particular but not exclusively, to the conversion of a hydrocarbon into a hydrogen-rich gas intended to supply fuel cells (PAC) either at low temperature of the proton exchange membrane type (abbreviated as PEM for “Proton Exchange Membrane ”), either at high temperature of the molten carbonate type (abbreviated as MCFC for“ Molten Carbonate Fuel Cell ”) or of the solid oxide type (abbreviated as SOFC for“ Solid Oxide Fuel Cell ”).
• PAC fuel cells
• the expression “lower calorific value” or PCI is defined below.
• the calorific value is defined as the quantity of heat released by the complete combustion of the fuel unit considered.
• the lower calorific value excludes from the heat given off, the heat of condensation of the water supposed to have remained in the vapor state after combustion.
• the hydrogen fuel can come from a pressurized or cryogenic tank. However, given the safety problems inherent in the storage of hydrogen, it is wise to obtain it from a fuel (hydrocarbon or alcohol), the hydrogen of which will be released as and when required.
• reformers using partial oxidation or steam reforming as a process generally include a high or low temperature “shift” unit (CO recycling), a steam generator, and a drying unit to remove excess steam.
• CO recycling high or low temperature
• steam generator steam generator
• drying unit to remove excess steam.
• the invention starts from the observation that pyrolysis overcomes these stages since it takes place in the absence of any source of oxygen thus preventing the formation of CO.
• the partial pressure of hydrogen in the gas formed is higher compared to other methods given, for example, the absence of nitrogen from the air used in partial oxidation.
• the fuel of choice is a hydrocarbon (methane, propane, butane) or a mixture of hydrocarbons.
• an alcohol can be envisaged at the choice for the cases where the production of synthesis gas, mixture of H 2 and CO, is required.
• Manikowski et al. propose a hybrid system composed of a catalytic pyrolysis reactor producing a hydrogen-rich gas and a mixture of combustible residues.
• the hydrogen-rich gas powers a fuel cell to generate electricity and mixture of combustible residues is burned in a combustion engine to produce mechanical power.
• This process treats various liquid fuels derived from petroleum. These fuels can be linear or branched alkanes with at least five carbon atoms but also all types of commercial fuels such as gasoline, kerosene ...
• the operating conditions chosen are such that only 20% of the hydrogen contained in the fuel is converted into the form of dihydrogen.
• Poirier et al. propose a pyrolysis process carrying out the catalytic decomposition of natural gas into a gas rich in hydrogen and carbon (MG Poirier, C. Sapundzhiev, Catalytic decomposition of natural gas to hydrogen for fuel cell applications, Int. J. Hydrogen Energy, vol. 22, No. 4, 1997, 429-433).
• the authors suggest the use of hydrogen-rich gas to power a PEM fuel cell.
• the catalytic bed on which the carbon formed during the pyrolysis reaction is deposited is then regenerated by burning the carbon with air.
• the authors propose a concept based on the use of two reactors operating alternately.
• the first operates in a pyrolysis regime to produce a hydrogen-rich gas while the second regenerates the catalytic bed by oxidation of carbon.
• the structure of the catalytic bed is designed to leave a dead volume sufficient to allow the accumulation of a large amount of carbon.
• PCI lower calorific value
• the pyrolysis of methane the main constituent of natural gas, is endothermic and requires an input of approximately 12% of the PCI of natural gas.
• the authors therefore propose to use the energy released by the combustion of carbon to provide the heat necessary for the decomposition of natural gas.
• the catalytic bed generates parasitic side reactions. Indeed, a production of CO is observed during the pyrolysis phase while no oxygen supply is carried out. This emission probably comes from the partial reduction of oxides present in the catalyst and formed during the regeneration phase.
• a propane pyrolysis system very similar to that of Poirier et al. was proposed by the German team of Ledjeff-Hey. It differs from it mainly by the nature of the hydrocarbon treated.
• K. Ledjeff-Hey N. Formanski, Th. Kalk, J. Roes; Compact Hydrogen Production Systems for Solid Polymer Fuel Cells, J. Power Sources, 71, 1998, 199-207
• K. Ledjeff- Hey, Th Kalk, J. Roes Catalytic cracking of propane for hydrogen production for PEM fuel cells, 1998 Fuel Cell Seminar, Palm Springs, California 1998.
• the pyrolysis reactors described above have serious shortcomings and shortcomings.
• the pyrolysis processes reveal an intrinsic difficulty: the lower calorific value (PCI) of the hydrogen produced is generally of the same order, or even lower than that of carbon and the other residues of pyrolysis.
• PCI calorific value
• the invention aims to eliminate these drawbacks. To this end, it offers a solution allowing the use of the pyrolysis mechanisms for other applications such as: - Pre-reforming for high temperature batteries of the molten carbonates (MCFC) and solid oxides (SOFC) type. - The co-generation of heat and electricity for housing either by coupling with a PEM type heat pump, or by coupling with a SOFC heat pump. - The production of synthesis gas for petrochemicals.
• MCFC molten carbonates
• SOFC solid oxides
• a process for producing a hydrogen-rich gas usable in a fuel cell this process consisting in carrying out, in a reactor, thermal cracking, without catalyst, for pyrolyzing a fuel chosen so to produce either a gas rich in hydrogen and free of carbon monoxide, or a gas rich in hydrogen and containing carbon monoxide.
• the effluent gases produced during the pyrolysis and inert with respect to the cell are used as fuel at the level of the burner for heating the reactor with a view to bringing it to the reaction temperature.
• the pulverulent carbon produced during the pyrolysis reaction can be burned either so as to produce carbon monoxide or CO, at least in part, or so as to produce carbon dioxide or C0 2 (heat) to complete the heating reactions and possibly providing a related heating system.
• the reactor can comprise two or more pyrolysis chambers used alternately. In this case, the chamber not used for pyrolysis is regenerated by the introduction of air which causes, at the right temperature, the combustion of the carbon deposited during the pyrolysis phase.
• the combustion chamber is placed at the very heart of the reactor (s); - The composition and the nature of the mixture feeding the burner are variable over time;
• the extraction and purification of hydrogen can be carried out using a permeable and selective hydrogen membrane
• the pyrolysis reactions are catalyzed by means of a plasma.
• the combustion chamber is placed at the very heart of the reactor or reactors in order to efficiently heat the reactive mixture at high temperature.
• composition and the nature of the mixture feeding the burner are variable over time.
• the priming will be done using the fuel used for the pyrolysis, then once the latter has started, the resulting co-products will be recycled to maintain the reaction in the burner.
• the carbon monoxide produced during the combustion of powdered carbon can also fuel the burner.
• a device for initiating combustion is provided in the burner by means of a plasma.
• Different means of plasma production are possible.
• the simplest method is to generate sparks between the electrodes of a spark plug similar to those used in the engines of motor cars.
• This ignition system When starting combustion in the burner, it is necessary to involve this ignition system. The latter can be stopped in steady state as soon as the temperature of the burner has reached a value allowing the auto-ignition of the combustible mixture.
• Efficient heat transfer structures between the burner and the pyrolysis chamber are provided.
• an excellent heat transfer must be ensured between the hot gases resulting from combustion in the burner and the very wall of the burner.
• This transfer is here made more efficient by increasing the contact surface of the metal with the hot gases by means of a metallic structure. It is shaped, in particular but not exclusively, fins, honeycomb or foam.
• This structure is arranged inside the burner and the contact with the internal walls of the latter is carried out so as to minimize the thermal resistance at this level.
• the heat transfer between the burner enclosure and the reactive gas circulating inside the pyrolysis reactor is optimized by means of a metal structure similar to the previous one, but arranged in contact with the external wall of the burner. .
• An optional method of operating the process consists in extracting the hydrogen from the reactor by means of hydrogen-permeable and selective membranes. Besides the advantage of producing a very pure hydrogen, this mode makes it possible to increase the yield of the process since the extraction of the hydrogen displaces the chemical equilibrium in the direction of a more complete reaction.
• the filter is made of a porous refractory material.
• One possible way of making this filter is to form a tampon made of refractory fibers, made of alumina wool for example.
• powdery carbon turns out to be an asset here. Indeed, several options are possible for its valuation. For example, it can, in small power plants, be collected for use as is in industry. It can also be oxidized in situ so as to constitute a source of heat via the production of carbon dioxide or electricity via the production of carbon monoxide.
• the CO produced can then be used as fuel in a SOFC type heat pump, thereby increasing the electricity yield.
• a plasma generator can be incorporated into the pyrolysis reactor.
• the plasma generates chemically very reactive radicals and plays a role comparable to that of a catalyst.
• the effect of this effect is in particular to accelerate the dehydrogenation reactions of different hydrocarbons.
• plasma generators can be used for this application, mainly "barrier" discharge and microwave discharge generators. Such devices have been described in the prior patent WO 98/28223.
• FIG. 1 is a pyrolysis device according to the invention intended to supply a low temperature PEM type heat pump
• FIG. 2 shows a pyrolysis device according to the invention intended to supply a high temperature heat pump of the SOFC type
• FIG. 3 shows a device comprising two reactors
• FIG. 4 shows a complete circuit incorporating the device of Figure 3;
• FIG. 5 shows a device using a polymer membrane operating at low temperature intended to purify the mixture rich in H 2 obtained
• FIG. 6 represents a device using a metal membrane operating at high temperature intended to purify the mixture rich in H 2 obtained
• FIG. 7 shows a device characterized in that the metal membrane is placed inside the pyrolysis reactor.
• FIG. 1 represents an example of a pyrolysis device according to the invention.
• This device here supplies a low temperature PEM fuel cell 1.
• this device comprises a single cylindrical reactor R heated by a cylindrical burner B incorporated at its heart so as to ensure excellent heat transfer, the reactor-burner assembly being placed in a heat-insulated cylindrical envelope 2 intended for limit thermal losses from the system.
• the reactor R is delimited by the cylindrical wall of the burner and by an external cylindrical wall coaxial with the burner. It is closed by a bottom FD in the form of a spherical cap and by an annular top DA located around the top of the burner.
• the pyrolysis reactor operates cyclically. It is indeed successively the seat of pyrolysis reactions which produce a gas rich in hydrogen and carbon oxidation reactions which make it possible to regenerate the reactor.
• the reactor R is heated by means of the burner B to a temperature allowing the cracking reactions of the hydrocarbon used. This temperature is around 550-650 ° C for propane and 700-800 ° C for methane.
• the fuel after a possible desulfurization, is introduced into the reactor R by means of the pipe. 3 located at the top of reactor R.
• Cracking by pyrolysis creates a gas rich in hydrogen and powdery solid carbon which is deposited in the reactor R.
• the alumina wool filter 4 located in the bottom of the reactor R, retains the carbon particles in the reactor and removes them from the hydrogen-rich gas extracted by the conduit 5 located on the other side of the filter 4.
• the hydrogen-rich gas Before being introduced into the anode compartment of the heat pump 1, the hydrogen-rich gas is cooled, by means of a heat exchanger 6, to a temperature compatible with this type of battery, about 50 ° C.
• the mixture of residual gases mainly unburned hydrogen and methane, is recycled to burner B by means of line 7.
• the burner B is a combustion chamber supplied at its top with fuel through the pipe 7 and with air through the pipe 8.
• An additional supply of fuel can be provided to provide additional heat.
• the combustion when the system is cold, is initiated by means of a plasma produced for example by an electric discharge between the electrodes of a spark plug of a combustion engine 9 situated at the top of the burner B.
• a plasma produced for example by an electric discharge between the electrodes of a spark plug of a combustion engine 9 situated at the top of the burner B.
• combustion self-ignition occurs and the plasma is no longer required.
• metallic structures 10 for example of the fin, honeycomb or metallic foam type are arranged on either side of the wall of the burner.
• the useful heat contained in the exhaust gases is recovered in a heat exchanger 12.
• the duration of the sequence of Pyrolysis is limited by the accumulation of powdery carbon in reactor R. This duration is variable depending on the parameters of the system. It can typically be 15 to 30 minutes.
• the regeneration phase a simple way to remove the carbon accumulated in the reactor R is to oxidize it to form a mixture of CO and C0 2 .
• a suitable and heated air flow through the heat exchanger 6 is introduced, at the top of the reactor R, by means of the conduit 13.
• the conduit 3 is then closed.
• the reactions of carbon with oxygen in the air are written:
• the heat released is recovered in the heat exchanger 6 before entering the burner B then the excess heat not transmitted through the walls of the burner is recovered by the heat exchanger 12 via the exhaust gases.
• this device can produce a maximum of 241 kJ of electricity per mole of methane, or 30% of the methane's PCI.
• the thermal energy recoverable from the exchangers is then 247 kJ.
• the maximum value of the overall PCI yield of heat + electricity production is therefore 61%.
• propane an electricity production of 482 kJ per mole of propane is obtained, ie 23.6% of the PCI of propane.
• the thermal energy recoverable from the exchangers would be 1180 kJ per mole of propane.
• the maximum value of the overall PCI output of heat + electricity production is then 81%. This example is given as an indication in order to define an order of magnitude of the powers released and the yields.
• FIG. 2 represents a pyrolysis device according to the invention coupled with a high temperature fuel cell 15 of the SOFC type. Its function is then to transform the fuel into synthesis gas (CO + H 2 ) directly usable by the PAC 15. This conversion upstream of the cell will be called pre-reforming. It is well known that the conversion efficiency of PACs of the SOFC type is improved when they are supplied with synthesis gas (CO + H 2 ) rather than directly with a hydrocarbon.
• the heat exchanger 6 located on the outlet 5 is no longer useful since the gases from the pyrolyzer can be introduced at high temperature into the anode compartment of the heat pump 15.
• the solenoid valves 14 have been eliminated because the heat pump 15 accepts CO and therefore does not need to be isolated during the regeneration phase.
• a solenoid valve EN1 makes it possible to convey the hot air to the burner B through the conduit 8 to maintain the combustion, or to the reactor R through the conduit 13 for the regeneration sequence.
• the PAC 15 accepts very well to be supplied with a mixture of H 2 + CO gas.
• the constraint of producing a gas rich in hydrogen and totally devoid of CO is no longer necessary in the present situation. It therefore becomes possible to widen the choice of fuel to be pyrolyzed and to extend it to ethanol or to other oxygenated fuels.
• the pulverulent carbon accumulated in the reactor R during the pyrolysis sequence must be gasified by oxidation.
• the mixture of CO + C0 2 gas produced during the regeneration in the reactor R can be sent directly to the anode compartment of the heat pump 15 via the outlet 5.
• the means of maximizing this ratio are to carry out a gentle combustion of the carbon, during the regeneration phase, in order to stop the reaction to the formation of CO, namely mainly:
• a SOFC type heat pump is considered to operate with an electrical conversion efficiency of 45%, and is supplied with the gases produced during the pyrolysis.
• the reactor is powered by methane and the pyrolysis reaction produces a complete conversion of this fuel. It turns out with the hydrogen produced that this device makes it possible to obtain a maximum of 217 kJ of electricity per mole of methane, or 27% of the PCI of methane.
• the electric production of the SOFC type heat pump adds an additional contribution of up to 127 kJ of electricity per mole of methane, i.e. 16% of the methane ICP. .
• Overall electricity production can therefore in principle reach 344 kJ of electricity per mole of methane, or 43% of the methane ICP. The production of thermal energy would be roughly equivalent.
• a co-generation system operating with methane according to this principle would therefore make it possible to produce substantially equal electrical power and thermal power with an overall efficiency (heat + electricity) of around 80%.
• the same propane-powered system could reach 434 kJ of electricity per mole of propane from the hydrogen formed, or 21% of the propane ICP. Electricity production from the CO formed could reach 381 kJ per mole of propane, or 18.7% of the PCI of propane. Overall electrical production can therefore in principle reach 815 kJ of electricity per mole of propane, or 40% of the propane ICP. In this case too, the production of thermal energy would be roughly equivalent to the production of electricity and the overall efficiency (heat + electricity) would reach around 80%.
• FIG. 3 represents a system with two reactors RI and R2 in order to obtain continuous and no longer cyclical operation.
• the two reactors are delimited by an external cylindrical wall and by the cylindrical walls of the burner B '.
• the reactors like the burner are respectively closed by a top and a bottom in the shape of a spherical cap.
• the reactor-burner assembly is placed in a cylindrical insulated envelope 16 intended to facilitate the high temperature maintenance of the pyrolysis reactors and to reduce the thermal losses of the system.
• the operating principles of the double pyrolysis chamber device are substantially identical to those previously stated with reference to FIGS. 1 and 2.
• the existence of two reactors makes it possible to operate one in the pyrolysis sequence while the other operates in regeneration sequence and vice versa.
• Burner B ' located at the heart of the system. It is cylindrical in shape and has in its middle a ferrule allowing an enlargement of the combustion chamber. This ferrule accommodates the ignition device 10 in the middle of the left side of the burner B 'and the passages of several conduits in the middle of the right side: an exhaust duct 17 collecting the smoke at the top of the burner B', a duct 18 supplying the burner with fuel at its base and a duct 19 supplying the burner with air at its base also.
• the two reactors RI and R2 are identical. Each of the two is connected to a fuel supply duct 20, an air supply duct 21 and a product discharge duct 22.
• the conduits 20 and 21 are placed in the upper part of the reactor and the conduit 22 in the lower part just above the conduits of the burner B.
• the conduits 20 and 21 are placed in the lower part of the reactor and the conduit 22 in the upper part just below the conduits of the burner B '.
• the heat transfer between the hot gases (fumes) from the burner B 'and each reactor is ensured by high-efficiency heat exchange structures 23 of the same type as those mentioned in the examples of FIGS. 1 and 2.
• Trapping of the particles of carbon produced by the pyrolysis reactions is carried out in the reactor RI and in the reactor R2 by filters 24 made of refractory fibers, for example made of alumina fibers, situated at the level of the conduits 22, on either side of the right part of the shell.
• This double reactor system can be used to continuously supply a PEM type fuel cell connected in a similar manner to the case shown in FIG. 1 or a SOFC type fuel cell connected in a similar manner to the case shown in FIG. 2.
• FIG. 4 is a representation of a complete circuit incorporating the device of FIG. 3. Here, only the gas supply circuits comprising solenoid valves controlled by an electrical control circuit will be described.
• the pyrolysis chambers (RI, R2) are supplied by two supply circuits:
• the two reactor gas outlet conduits converge on a set of two three-way solenoid valves, EN4 and EN5, which can send the gases produced during pyrolysis and during the partial combustion of carbon, to the heat pump for solenoid valve EN4 and in the burner for solenoid valve EV5.
• the burner is supplied with air by the same supply circuit as the pyrolysis chambers but upstream of the solenoid valve EN3 and with fuel via either solenoid valve EV5 as described above or an solenoid valve EN6 regulating the arrival at the choice of the gases from the heat pump or fuel through an outlet upstream of the EN2 solenoid valve.
• FIGS. 5, 6 and 7 describe a variant of the device, object of the invention, consisting in incorporating, before the heat pump, a membrane for purifying hydrogen in the circuit for extracting the gases produced by pyrolysis.
• the system can thus be used as a generator of very pure hydrogen.
• - metal membranes These are very selective membranes made of a metal very permeable to hydrogen, generally an alloy of palladium. These membranes can be used at high temperature, typically 500 to 550 ° C. They can therefore be integrated either in the high temperature gas circuit (Fig. 6), or in the reactor itself (Fig. 7).
• FIG. 5 represents a device using a polymer membrane 25.
• the device is similar to that of FIG. 1 except on the following points:
• the membrane 25 is interposed between the heat exchanger 6 and the fuel cell;
• the mixture of hydrogen-rich gas, extracted from the reactor through line 5, then cooled to less than 120 ° C by means of the exchanger 6 is sent to the membrane purifier 25. It comes out in two ways.
• the first channel NI routes the very pure hydrogen thus extracted to the PEM fuel cell to supply it and the second channel N2 evacuates the residual gases which are recompressed using the heating compressor 26 so as to be recycled with the fuel supplying the pyrolysis reactor via line 3.
• FIG. 6 represents a device using a metallic membrane 27 made of palladium alloy operating at high temperature. This device is similar to that of FIG. 4 except for the fact that the membrane purifier 27 is located before the heat exchanger 6. The very pure hydrogen thus extracted is sent to the fuel cell of PEM type after having been cooled by means of the heat exchanger 6. The residual gases are recompressed by means of the compressor 26 so as to be recycled with the fuel supplying the pyrolysis reactor via line 3.
• FIG. 7 represents a device having a metal membrane 28 placed inside the pyrolysis reactor itself.
• This palladium alloy membrane operates at high temperature, typically at 500-550 ° C and has the shape of a cylindrical pencil.
• the latter is protected by a sleeve 29 of refractory fibers, an alumina fabric for example. The purpose of this sleeve is to keep the carbon particles away from the membrane.
• the pyrolysis reactor R can contain, if necessary, several identical membranes so as to increase the surface area of active membrane and thereby the flow of extracted hydrogen.
• co-generation boilers heat and electricity
• recreational vehicles camping cars, caravans
• the power level of a co-generation module will be approximately 5 kWe + 5 kWth.
• the fuels to be used will be: natural gas, propane, heating oil, etc.

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• 2001
  • 2001-07-17 FR FR0109635A patent/FR2827591B1/fr not_active Expired - Fee Related
• 2002
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