Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
  • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
  • C10J3/60—Processes
  • C10J3/64—Processes with decomposition of the distillation products
  • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
  • C10J3/02—Fixed-bed gasification of lump fuel
  • C10J3/20—Apparatus; Plants
  • C10J3/30—Fuel charging devices
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
  • C10J3/02—Fixed-bed gasification of lump fuel
  • C10J3/20—Apparatus; Plants
  • C10J3/34—Grates; Mechanical ash-removing devices
  • C10J3/40—Movable grates
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2200/00—Details of gasification apparatus
  • C10J2200/15—Details of feeding means
  • C10J2200/158—Screws
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
  • C10J2300/0953—Gasifying agents
  • C10J2300/0973—Water
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
  • C10J2300/0983—Additives
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
  • C10J2300/0983—Additives
  • C10J2300/0986—Catalysts
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
  • C10J2300/1861—Heat exchange between at least two process streams
  • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas

Definitions

• the present invention includes a process for producing integrated hydrogen (H 2 ). It also relates to a system implementing the method according to the invention.
• the field of the invention is the field of synthesis gas production from organic material and more particularly the field of production of H 2 .
• the synthesis gas obtained after gasification comprises H 2 and carbon monoxide (CO) in variable proportions and a priori not determinable and mixed with other compounds.
• An object of the invention is to provide a method and a system for producing H 2 from organic matter irrespective of the moisture content of the organic material.
• Another object of the invention is to propose a system for producing H 2 from plant biomass in the form of a single set, integrated, complete and less expensive than current systems.
• Another object of the invention is to provide a method and system for producing H 2 from plant biomass for controlling the proportion of H 2 produced.
• the invention thus proposes a process for producing hydrogen (H 2 ) from organic material, the process comprising the following steps:
• the gaseous treatment stream essentially comprises heat-exchange CO 2 .
• Pyrolysis produces, on the one hand, a gaseous pyrolysis stream comprising the gaseous treatment stream, water vapor (H 2 O) and volatile organic compounds (VOCs) originating from the organic material, and on the other hand pyrolysis coals comprising carbon elements; oxycombustion of said volatile organic compounds present in the gaseous pyrolysis stream, by oxygen injection, upstream of a layer of oxido-reducing filter material comprising carbon elements at high temperature; and
• the method according to the invention makes it possible to produce hydrogen from organic matter, irrespective of the moisture content of the organic matter, it integrates the prior drying of the organic matter, in order to recover the vapor of the organic matter. water and inherent energy during the pyrolysis step. Thus, it is not necessary, in the process according to the invention, for the organic material to undergo prior treatment, for example drying, to reduce the moisture content of the organic material.
• the process according to the invention makes it possible to treat the heavy compounds present in the pyrolysis gas. These are cracked during the oxycombustion of VOCs.
• the oxido-reducing layer may advantageously comprise oxides in a reduced form. These oxides deoxidize part of the water vapor (H 2 O), the deoxidation producing elements of hydrogen (H 2 ). After deoxidation, the oxides are in an oxidized form.
• the deoxidation of the water vapor by the oxides in a reduced form is according to the following reaction:
• the oxides are activated or oxidized.
• at least a part of the oxides in an oxidized form obtained from the deoxidation of the water vapor according to the reaction described above in the redox layer, is used for oxidation of volatile organic compounds (VOCs). upstream of the redox layer.
• VOCs volatile organic compounds
• the oxides are again in a reduced form. At least a portion of these oxides in a reduced form is again used in the redox layer for further deoxidation of the water vapor.
• the process according to the invention comprises a looping of the oxides, between the redox layer where these deactivated oxides are activated by deoxidation of the water vapor, and a VOC oxidation zone where the activated oxides are deactivated following oxidation of the VOCs.
• the oxycombustion is carried out by injecting oxygen, O 2 , upstream of the oxido-reducing layer.
• the oxidation of VOCs by oxides is endothermic and is flameless while the oxycombustion of VOCs is exothermic and occurs with flames.
• the process according to the invention requires a good balance between the oxidation of VOCs by oxides and the oxycombustion of VOCs by injection of O 2. .
• the equilibration is done by the oxidation of oxides in an oxidized form according to the organic matter. The thermal equilibrium is achieved by oxycombustion of a part of the VOCs.
• the following oxides can be used in the present invention: Fe2O3, NiO, CuO, CoO, CeO, ZnO, CaO, MgO, TiO2, Al2O3.
• these oxides are given as non-limiting examples.
• combinations of oxides can be used.
• Non-limiting examples of combinations of oxides are Fe 2 O 3 / CaO, NiO 2 / Al 2 O 3, CuO / TiO 2, CoO / MgO, CoO / CaO.
• the synthetic gas stream may further comprise carbon monoxide (CO) and water vapor (H 2 O).
• the method according to the invention may comprise, in this case, a lowering of the temperature of the synthesis gas stream downstream of the redox layer. This lowering of temperature is achievable by the interposition of at least one heat exchanger which will also have the purpose of absorbing the exotherm of the oxidation-reduction reaction, called water-shift, which is thus made possible between the monoxide of carbon (CO) and the vapor (H 2 O), producing H 2 and CO 2 according to the equation:
• the process according to the invention makes it possible, by means of this step of reducing water vapor by carbon monoxide compounds, to control and vary the proportion of H 2 produced in the synthesis gas stream.
• the synthesis gas stream may comprise residual steam, not reduced depending on the initial wet organic load.
• the process according to the invention can comprise a separation of the water vapor from the other components present in the synthesis gas stream by condensation of the water vapor. This condensation can be achieved by reducing the temperature of the synthesis gas stream to the condensation temperature of the water vapor.
• the synthesis gas stream in principle comprises hydrogen, carbon dioxide and the treatment gas stream.
• the process according to the invention may then comprise a step of separating the hydrogen H 2 present in the synthesis gas stream.
• This separation can be done by techniques known to those skilled in the art, for example a membrane system of molecular separation.
• the residual synthesis gas stream essentially comprises CO 2 .
• At least a portion of this CO 2 can be reused as a process gas stream for pyrolysis of a new charge of organic material after heating.
• At least a portion of the CO 2 obtained thus becomes the heat transfer stream for the pyrolysis of a new load of organic matter.
• the lowering of the temperature of the synthesis gas stream downstream of the redox layer may comprise a transfer of thermal energy from this synthesis gas stream to at least a portion of the treatment gas stream, thereby bringing said stream gaseous treatment at a pyrolysis temperature of a material charge organic.
• the method according to the invention may comprise a looping allowing a continuous reuse of the treatment gas stream for the pyrolysis of the organic material.
• the reused CO 2 is recycled continuously and is not released into the atmosphere.
• the lowering of the temperature of the synthesis gas stream downstream of the redox layer may further comprise a transfer of thermal energy to circulating liquid water, thus achieving a change of state of said liquid water to obtain superheated steam.
• the method according to the invention may further comprise a step of adding, to the gaseous stream of oxidized pyrolysis, the water vapor. This water vapor can be that obtained above.
• the oxidized pyrolysis gas stream may be enriched with water vapor, either to compensate for the low humidity of the organic material and to increase the quantity of H 2 obtained, or to adjust the H 2 ZCO ratio.
• the amount of residual water vapor in the synthesis gas stream must be large enough to achieve the water shift reaction described above.
• At least a portion of the pyrolysis chars generated in the pyrolysis step can be used to form at least part of the layer of redox-reducing filter material.
• This pyrolysis step can be done gradually in the form of sub-steps, these sub-steps performing the progressive gasification of the organic material.
• the pyrolysis step can be: - preceded by a previous step of dehydration of the organic material, and / or
• a system for producing hydrogen from organic material comprising a single enclosure comprising: a first reactor for pyrolysis of a charge of organic material by passing through said organic material having a treatment gas stream essentially comprising heat-carrying CO 2 , said pyrolysis providing, on the one hand, a gaseous pyrolysis stream comprising said gaseous treatment stream, water vapor (H 2 O) and volatile organic compounds (VOCs), and secondly pyrolysis coals comprising carbon elements, and - a second reactor comprising:
• VOCs CO 2 , H 2 O, etc.
• the system according to the invention makes it possible to produce, in a single integrated enclosure, in the form of a monobloc assembly, hydrogen from wet organic materials, for example wet biomass, unlike current installations.
• the biomass and / or the organic material is first treated in temperature in a first chamber to reduce its humidity, and then transported in a second chamber for the generation of hydrogen.
• the first reactor comprises at least one gate on which is disposed the organic material to be pyrolyzed.
• the first reactor may comprise a plurality of grids, arranged one under the other, each of said grids being adapted to:
• the gaseous treatment stream is directly injected into the heart of the organic material on each grid.
• Each of the grids of the first reactor comprise one or more orifices distributing the gaseous treatment flow to the organic material on this grid.
• the organic material arranged on a grid is also traversed by the gaseous treatment stream from the lower grids.
• Each of the grids can also be mechanized.
• first and the second reactor are separated by a double wall forming a communication connecting the upper part of the first reactor to the lower part of the second reactor, said communication authorizing: the passage of the gaseous pyrolysis stream from the upper part of said first reactor to the lower part of said second reactor, and
• the layer of oxido-reducing material may further comprise oxides in a reduced form and participating in the deoxidation of the water vapor passing through this layer, the deoxidation of the water vapor by the oxides producing dihydrogen (H 2 ) and oxides in an oxidized form.
• the oxidation zone of the volatile organic compounds may further comprise one or more oxygen injectors arranged to inject the oxygen necessary for an oxycombustion of at least a part of the volatile organic compounds in said oxidation zone.
• the oxidation zone of the volatile organic compounds may further comprise one or more oxygen injectors (with an ignition device) arranged to inject the oxygen necessary for an oxycombustion of at least a part of the volatile organic compounds. upstream of said oxidation zone.
• the grid supporting the layer of oxido-reducing material is arranged to allow the flow of the oxides in an oxidized form to the oxidation zone of the volatile organic compounds, at least a portion of the volatile organic compounds being oxidized by said oxides in an oxidized form.
• the oxides which are at high temperature in the redox layer are transferred to the VOC oxidation zone naturally and without manipulation.
• the oxidation zone of the volatile organic compounds (VOCs) may further comprise one or more grids, arranged one under the other, and provided for slowing the flow of the oxides in an oxidized form so as to improve the oxidation of the compounds volatile organic compounds (VOCs) by oxides in an oxidized form.
• the system according to the invention may further comprise a transfer device carrying out a transfer:
• the synthesis gas stream may comprise carbon monoxide (CO) and water vapor (H 2 O).
• the system according to the invention further comprises at least one heat exchanger arranged to lower and control the temperature of the synthesis gas stream. This lowering temperature allows a redox reaction, called water-shift, between carbon monoxide (CO) and water vapor (H 2 O) producing H 2 and CO 2 .
• the system according to the invention may comprise: a first exchanger designed to perform a heat exchange of the synthesis gas stream to the treatment gas stream, and a second exchanger designed to perform a heat exchange flow gaseous synthesis to liquid water producing water vapor.
• the water vapor obtained can be used to enrich the pyrolysis gas stream with water vapor in the case where the organic material pyrolyzed in the first reactor has a moisture content that is too low.
• the system according to the invention further comprises means for separating hydrogen from the synthesis gas stream.
• FIG. 1 is a schematic representation of a method according to the invention
• Figure 2 is a schematic representation in a sectional view of a system according to the invention.
• FIG. 3 is a schematic representation in a rear view of the system of Figure 1;
• Figure 4 is a schematic representation in a top view of an oxycombustion zone in the system of Figure 2;
• Figure 5 is a representation in a sectional view of the oxyfuel zone of Figure 4;
• FIG. 6 is a diagrammatic representation in a view from above of a grid implemented in the system of FIG. 2;
• Figure 7 is a schematic representation in a sectional view of the grid of Figure 6;
• FIG. 8 is a schematic representation in a sectional view of a bar of the grid of FIG. 6.
• Figure 1 is a representation of an example of different steps of a method according to the invention.
• MO organic matter more or less wet, is introduced into a first reactor and a FT treatment gas stream which essentially comprises heat-exchange CO 2 .
• the organic matter MO contains 50% moisture, it can be freshly cut biomass / collected biomass or any other biomass or organic material, having an energy value.
• the treatment gas stream FT is previously brought to its treatment temperature allowing the pyrolysis of the organic materials MO.
• the processing temperature is defined by the characteristics of the gasifiable compounds of the organic material MO and the characteristics of the desired pyrolysis coals.
• step 100 the organic material is subjected to pyrolysis.
• the pyrolysis is carried out in the form of several sub-steps including:
• the first is a sub-step of dehydration of the organic matter
• a pyrolysis gas stream FP comprising the treatment gas stream FT, that is to say essentially CO 2 , the H 2 O water vapor from organic matter and volatile organic compounds VOCs also from organic matter MO, and
• the pyrolysis gas stream FP and the carbon elements C are transferred as the pyrolysis proceeds to a second reactor and will be treated as described below.
• the pyrolysis coals are homogeneously mixed with oxides in a reduced or deactivated form Me, the mixture is then deposited on a grid in the second reactor to form a layer of redox-reducing filter material.
• the carbon elements C and the deactivated oxides Me are provided to carry out deoxidation of the water vapor which passes through this oxido-reducing layer as described below.
• the deactivated oxides Me are activated MeO following this deoxidation and are transferred to a deoxidation zone.
• the pyrolysis gas stream FP passes through, at step 102, an oxy-fuel combustion zone of a portion of the VOCs and an oxidation zone of another portion of the VOCs present in this pyrolysis gas stream FP.
• VOCs undergo at least in part:
• these activated oxides MeO are the oxides mixed with the pyrolysis coals in the oxidation-reduction layer in a deactivated form Me which were first activated (oxidized ) following the deoxidation of the water vapor H 2 O as described above, then transferred to the VOC oxidation zone.
• the oxidized pyrolysis gas stream FPO comprises CO 2 and water vapor H 2 O.
• the deoxidation of the activated oxides MeO in favor of VOCs is endothermic and produces deactivated oxides Me which are re-transferred into the layer of redox material after having been homogeneously mixed with new pyrolysis coals produced by pyrolysis. a new charge of organic matter in the first reactor.
• Oxygen is a particular oxidation, exothermic, and produces a significant thermal energy. Part of this thermal energy makes it possible to maintain the oxidation zone at a temperature sufficient for the deoxidation of the activated oxides MeO and to bring the water vapor contained in the oxidized pyrolysis gas stream to the correct temperature for the operation of it is deoxidized by the layer of redox filter material formed by the carbon elements C and the deactivated oxides Me. Another part of this thermal energy is transferred, as the oxycombustion proceeds, to the gaseous pyrolysis stream coming from the first one. reactor. The pyrolysis gas stream thus acquires an additional heat capacity that promotes oxycombustion or oxidation as soon as it arrives in the second reactor.
• thermal energy ET1 of this thermal energy is transferred as oxyfuel combustion to the layer of redox filtering material formed by carbon elements C and the deactivated oxides Me.
• This thermal energy ET1 makes it possible to wear the layer lower of this redox layer at high temperature, about 100O 0 C.
• the complete oxycombustion occurs in the present example upstream and in the vicinity of the redox layer.
• the transfer of thermal energy ET1 to the redox layer is done naturally and without loss.
• step 104 the oxidized pyrolysis gas stream FPO passes through the layer of redox filter material formed by the carbon elements C and the deactivated oxides (or in a reduced form) Me.
• the water vapor H 2 O contained in this gas stream FPO is then in the required conditions and subjected to the strong redox characteristic of the elements of the layer of filtering material to be in turn deoxidized by the carbon elements C and the deactivated oxides Me of the lower layer of the redox oxide layer at high temperature, according to the following reactions:
• This deoxidation which produces hydrogen H 2 and carbon monoxide, is endothermic whereas the consequent oxidation of the deactivated oxides Me is very exothermic.
• the thermal balance is in excess, the exotherm is defined beforehand by the choice of the proportion of oxide materials Me which will be active in the process according to the invention.
• This exotherm allows in particular to carry and maintain the layer of redox filtering material, formed by carbon elements C and the deactivated oxides Me (or in a reduced form), as well as the water vapor (and consequently the gas flow in which it is located), at the optimum temperature of redox reaction.
• Part of this exotherm is also used in the configuration of the system according to the invention to raise the temperature of the pyrolysis gas stream passing through the double wall of the two reactors.
• synthesis gas stream FS Downstream of the redox layer, there is then a synthesis gas stream FS, at high temperature, comprising CO 2 , hydrogen H 2 , carbon monoxide CO and residual water vapor H 2 O.
• step 106 the temperature of this synthesis gas stream FS is lowered by thermal energy recovery.
• the reduction of the temperature of the synthesis gas stream FS is adjusted so as to carry out a so-called water-shift (or CO-sh ift) reaction consisting in the deoxidation of the water vapor H 2 O by the monoxide elements. of CO carbon, depending on the reaction:
• water vapor H 2 O 9 Part of this water vapor can be reinjected into the oxidized pyrolysis gas stream FPO upstream of the layer of oxido-reducing material, firstly to increase the amount of hydrogen H 2 obtained at the exit of the layer redox and secondly to have enough water vapor H 2 O 9 downstream of this layer to make possible the CO shift reaction described above.
• step 106 the carbon monoxide CO molecules present in the synthesis gas stream FS reduce the water vapor molecules H 2 O 9 .
• This step 106 that is to say the water shift reaction, is used to vary the proportion of H 2 in the synthesis gas stream and to obtain a determined proportion of H 2 in the synthesis gas stream FS.
• the synthesis gas stream no longer includes CO molecules.
• the synthesis gas stream thus comprises hydrogen H 2 , carbon dioxide CO 2 and residual water vapor H 2 O.
• stage 1 a small amount of residual water is recovered from condensation.
• Thermal energy ET3 is recovered at this stage and can be upgraded by any means known to those skilled in the art.
• the gas treatment flow FT, carbon dioxide CO 2 and hydrogen H 2 present in the synthesis gas stream FS are then separated in step 112 by any system known to those skilled in the art.
• Part of the recovered CO 2 is reused as a new FT gas stream for the pyrolysis of a new charge of organic material.
• this gaseous treatment flow FT must be brought to the pyrolysis time of 400/700 ° C envi ron.
• the rise in temperature of the treatment gas stream FT is carried out at step 108 by virtue of the thermal energy ET2 recovered during step 106, ie by reducing the temperature of the synthesis gas stream FS to bring it to the water-shift reaction temperature described above.
• the surplus of CO 2 recovered in step 112 can be condensed and stored.
• the hydrogen H 2 obtained can also be stored or used in energy production devices or systems coupled to the system according to the invention.
• 100% of the thermal energy, a component of the organic material MO, and 100% of the thermal energy, used in the desiccation and pyrolysis reactions of the organic material MO are transposed into available energy in the form of hydrogen H 2 , deductions made of losses and energy useful to the process.
• FIGS. 2 and 3 are schematic representation of a system according to the invention and Figure 3 is a representation of this system in a rear view.
• the system represented in FIGS. 2 and 3 comprises, in a single enclosure E, a first reactor 20 and a second reactor 30.
• the reactor 20 is the pyrolysis reactor built under pyrolysis heat transfer gas flow consisting essentially of CO 2 .
• This reactor 20 comprises a chute 200 through which the organic material MO is introduced into this reactor 20.
• the material MO then passes through four mechanical mills 201-204 defined four or four zones and having distribution orifices of a gas treatment flow FT at the heart of the organic material disposed on these grids.
• the treatment gas stream is conveyed to the four grids by a double wall 205.
• the organic material flows by gravity from a grid to a lower grid and undergoes a gradual temperature rise as it passes through. a grid to a lower grid.
• the organic matter MO is first retained by the first grid
• the 201 mechanized. It is dehydrated by the hot treatment gas stream coming from the double wall 205 which surrounds the pyrolysis reactor 20 on three sides and distributed through the orifices of the grid 201. It is also subjected to the reaction of the treatment gases from the bearings or grids lower 202-204.
• the grid 201 as well as the grids 202-204 are configured to allow the passage of the treatment gases from the lower grids and the flow of the organic material thus treated on the lower grids.
• the gate 202 receives the organic matter flowing from the gate 201 and the gate 203 receives the organic material flowing from the gate 202.
• These gates 202 and 203 constitute bearings carrying out the progressive pyrolysis of the organic material. The pyrolysis is thus carried out in cascade according to the number of steps or grids relative to the size of the system to the last grid, here the grid 204.
• the wire 204 is a parent where the organic material is superheated to reduce it to the non-gasifiable portion or to be carbonized and produce pyrolysis coals comprising carbon elements.
• the volatiles of the organic matter are completely gasified, thus finalizing the pyrolysis of the organic materials so that only the pyrolysis coals remain.
• the zone 206 comprises at its low point a mechanical collecting device 207, for example an Archimedean screw, which supports the pyrolysis coals and bring them to a transhipment device 208.
• a mechanical collecting device 207 for example an Archimedean screw
• the pyrolysis gas stream FP comprising the water vapor H 2 O 9 contained in the organic raw material, the heat-treating CO 2 and the volatile organic compounds VOC are aspirated by a general extraction mechanism (not shown). through an opening 209 in the upper part of the pyrolysis reactor 20.
• This pyrolysis gas stream FP is at the pyrolysis temperature and is sucked towards the reactors 30 via the double wall 210 concomitant with and communicating with the reactor 30.
• the cited double wall 210 is adjacent to the two reactor systems 20 and 30, and forms the fourth wall of the pyrolysis reactor 20.
• the space thus configured is equipped with devices for rapid thermal exchange between the wall of the reactor 30 and the pyrolysis gas stream from the pyrolysis reactor 20.
• the pyrolysis gas fl ux acquires a temperature conducive to self-ignition before they enter the reactor 30.
• the system further comprises motorization means 211 of the grids 201-204.
• the reactor 20 further comprises openings 212 arranged below the gate 204 which distributes the treatment gas stream FT.
• the zone 206 for collecting (receiving) the pyrolysis coals is profiled for the best flow of the materials towards the collecting device 207.
• the reactor 30 receives the FP pyrolysis gas stream and after treatment of this stream produces a FS synthesis gas stream comprising hydrogen H 2 .
• This reactor 30 is composed, in the present example, of three main zones.
• a first zone of deoxidation of water vapor comprising a grid 301 on which a layer of redox material 302 is disposed.
• This layer of oxido-reducing material is composed of pyrolysis coals poured onto the grid 301 by the cooling device.
• transhipment 208 see Figure 3, by an opening 303 arranged above the grid 301, after being mixed with oxides in a deoxidized form or homogeneously deactivated oxides.
• the carbon elements and the deactivated oxides are provided to carry out the deoxidation of the water vapor H 2 O passing through this layer 302. This deoxidation leads to an activation of the deactivated oxides, that is to say their transition to an oxidized form .
• the activated oxides are then transferred to a second zone of the reactor 30 which is the VOC oxidation zone.
• the activated oxides participate in the oxidation of the VOC volatile organic compounds in this zone 304.
• the VOC volatile organic compound oxidation zone 304 is upstream and downstream of the 301 lag and the 301 is configured to allow the upward flow of the gaseous stream from the VOC 304 oxidation zone and the flow of the solids. incombustible contained in the load which is constituted on this grid 301.
• the pyrolysis gas stream FP comprising volatile organic compounds enters the reactor 30 through the developed opening 300 which opens into the lower part of the VOC oxidation zone 304.
• This oxidation zone 304 is arranged in such a way as to organize the complete oxidation of the VOCs contained in the gas stream of pyrolysis. Grids 305 and 306 are suitably distributed to slow down the gravitational flow of the activated oxides and to allow complete oxidation of the VOCs in contact with these activated oxides in this zone 304.
• This stoichiometric oxidation can be advantageously prepared by an oxyfuel combustion.
• the opening 300 may also be called the oxycombustion zone of the VOCs and is upstream of the zone of oxidation of VOCs by activated oxides 304.
• the oxidation zone, in the broad sense, of the VOCs corresponds to:
• the temperature of the oxidized gas complex is not satisfactory at the exit of the zone 304, for an immediate reaction in contact with the oxy-d-reducer co-heat, it will be supplemented by the oxyfuel combustion of a portion of the carbons composing the low layer of redox material by an oxygen injection by an oxygen injector 308 arranged at the gate 301 supporting the layer of redox material.
• VOCs The combustion of these VOCs is carried out without flame in the case of a use of oxides and with flame in the case of the use of oxidizing oxygen. This combustion is totally controlled by 316 temperature probes and a 317 ignition and flame control system 318. In case of use of oxides, the reaction is endothermic, the control is achieved by partial oxycombustion of VOCs under zone 304.
• the configuration of the reactor 30 is defined in its lower part by a device 309 for separating the solids coming from the oxido-reducing layer and passing through the oxidation zone of the VOCs 304: deactivated minerals and oxides Me.
• a separation device 309 can for example being a vibrating carpet.
• the minerals are evacuated to the surface of the separation device 309 to a receptacle where they are supported by a sealed evacuation device 310.
• the deactivated oxides flow by gravity to a zone 311 for collecting the oxides deactivated by the VOCs. .
• This zone is profiled for better collection of deactivated oxides and includes a collection device.
• the deactivated oxides are supported by a transfer system 312 to be directed to the transfer system 208, where they will be brewed with the pyrolysis coals for intimate mixing and returned to the gate 301 through the opening 303.
• the oxidized pyrolysis gas stream passing through the layer of oxido-reducing material 302 contains only water vapor H 2 O 9 and CO 2 .
• the water vapor H 2 O 9 contained in the gaseous pyrolysis stream will exchange its oxygen atom O with the non-active carbons and oxides of the layer 302 to form H 2 and CO and active oxides MeO.
• the reaction is exothermic if the layer 302 contains oxides while it is endothermic if the layer contains only pyrolysis coals.
• the oxygen injector 308 provides additional oxygen under the grid 301 in order to provide a thermal compensation base.
• the oxides capture the thermal energy of the VOCs by oxidizing them to transport it within the oxidoreductive layer where it is transferred to capacitive energy for the reaction of deoxidation of H 2 O by the pyrolysis carbons.
• the oxides / VOC reaction enables the energy of the VOCs to be completely transferred to the Me oxides, allowing their substitution in the medium of deoxidation of H 2 O by Me, which an ordinary thermal reaction of the VOCs could not do. even under oxidizing oxygen.
• This secondary reaction by the oxides allows the most important transfer of the energy contained in the organic matter to the production of synthetic hydrogen, it is recyclable continuously.
• a synthesis gas stream FS comprising H 2 , CO, CO 2 and H 2 O 9 (superheated steam).
• the pyrolysis coals are reduced to the minerals contained in the organics of origin and the Me oxides are activated MeO, they are at the optimum temperature favoring the reaction with the VOCs in the VOC oxidation zone 304.
• heat exchangers are provided, the first being the concomitant double wall 210 in which the gaseous pyrolysis unit circulates.
• Two other exchangers 313 and 314 are situated in the upper part of the reactor 30 which composes the third main zone of this reactor 30.
• the synthetic gas stream gives up its heat energy, allowing and facilitating the shift reaction of CO on H 2 O in H 2 and CO 2 , if necessary.
• the synthesis gas stream exits the reactor 30 through an extraction opening 315.
• the synthetic gas stream leaving the opening 315 is essentially composed of H 2 , CO 2 and H 2 O, which are easily separable.
• This synthesis gas stream is extracted from the reactor 30 by a general extraction system (not shown).
• liquid water H 2 0 L can be introduced into the exchanger 314 to be vaporized and to provide water vapor H 2 O 9 in order firstly to regulate the exothermicity of the reaction in the layer of oxidizing filter material reducing agent 302 and the thermal reaction of CO-shift, and secondly to be used as water vapor to deoxidize.
• the system further comprises a distributor / weir (not shown) pyrolysis coals can be mixed with deactivated oxides. These materials are thus distributed and mixed so homogeneous and deposited on the gate 301 in an oxidoreductive charge defined according to the sizing of the system.
• FIG. 4 is a schematic representation in a top view of the double wall 210 and Figure 5 a representation of this wall in a sectional view along AA.
• this double wall comprises at its bottom part an opening 300 at which an oxy-combustion of VOCs is produced by injection of O 2 by an injector 307.
• the wall comprises a bay 41 into which the oxygen injector 307 opens.
• This rack comprises a gate 42 regulating the flow of the FP pyrolysis gas stream and improving the combustion of the VOCs.
• Figure 6 is a schematic representation in a top view of one of the grids 201-204.
• the grid shown in Figure 6 is arranged to receive the organic material, allow the upward flow of the gas stream in the reactor 20 and the gravity flow of incombustible solids contained in the organic material.
• This grid arranged to receive the organic materials is composed of several bars 61.
• FIG. 7 gives a sectional view of the FIG. 6 grid according to BB and FIG. 8 a sectional view of a bar 61.
• Each of the bars 61 comprises teeth 62, in contact with the members of the neighboring bars, and training each other during the rotation. Indeed, during rotation the teeth 62 of a bar 61 engrain with the teeth of a neighboring bar and drive it in rotation. During their rotation, the teeth 62 of the bars also cause the organic material disposed on the grid.
• each of the bars 61 has a hollow cylindrical body conveying the gaseous treatment flow.
• the gaseous treatment stream is injected into the heart of the organic material disposed on the grid through openings 63 arranged on the cylindrical body of each of the bars 61.

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• 2009
  • 2009-01-21 WO PCT/FR2009/050080 patent/WO2009098418A2/fr active Application Filing
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