WO2019034819A1 - Réacteur de méthanation biologique - Google Patents
Réacteur de méthanation biologique Download PDFInfo
- Publication number
- WO2019034819A1 WO2019034819A1 PCT/FR2018/052038 FR2018052038W WO2019034819A1 WO 2019034819 A1 WO2019034819 A1 WO 2019034819A1 FR 2018052038 W FR2018052038 W FR 2018052038W WO 2019034819 A1 WO2019034819 A1 WO 2019034819A1
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- WO
- WIPO (PCT)
- Prior art keywords
- water
- reactor
- carbon dioxide
- enclosure
- dihydrogen
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M25/00—Means for supporting, enclosing or fixing the microorganisms, e.g. immunocoatings
- C12M25/16—Particles; Beads; Granular material; Encapsulation
- C12M25/20—Fluidized bed
-
- 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
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Definitions
- the present invention relates to a fluidized bed biological methanation reactor. It applies, in particular, to the field of industrial methanation to produce a gas rich in synthetic methane by conversion of carbon dioxide and dihydrogen.
- Biological methanation technologies are sometimes used to increase the methane content of biogas from biological methanation.
- Biological methanization produces a biogas rich in methane and carbon dioxide and contains a number of minor compounds from fermentation such as ammonia, hydrogen sulfide, siloxanes and others.
- the proportions between methane and carbon dioxide vary from one methanization to another, but the 50/50 ratio gives an order of magnitude of the relative amounts of these two major constituents.
- the production of carbon dioxide during the methanation is inevitable, but it represents a significant part of the carbon initially introduced into the non-methanized methanizer into methane and it is also a compound that must be removed if it is desired to inject the methane in the natural gas network.
- thermochemical methanation the reaction is carried out in the gaseous phase at high temperature (at a temperature of about 300 to 400 ° C.) under greater or lesser pressure and in the presence of a catalyst.
- biological methanation the reaction is carried out in the liquid phase by means of methanogenic microorganisms of the Archaea domain, for example.
- the bacterial bed is a reactor that uses a carrier material for the development of microorganisms and this material is sprinkled with water to maintain the wet environment and to allow the transfer of gaseous reactants into the water for access by microorganisms.
- the reactive gas is introduced through the base of the reactor.
- the bacterial bed (as described in DE 10 201 10571 836) is characterized by a countercurrent circulation of the liquid and gaseous flows.
- the gas tends to circulate according to a so-called piston model which promotes the efficiency of the reaction.
- the circulation can be hampered by bacterial growth on the supports and induce preferential passages.
- the gas flow rate is relatively low to allow sufficient contact time between the reagents and microorganisms immobilized on the support.
- the bacterial bed is characterized by relatively low production rates (1.17 Nm 3 CH 4 / m 3 / day) and therefore a large footprint and bulk volume. This size is related to the fact that it is necessary to maintain a large empty volume to leave free passages to gas and liquid and not to clog the support material.
- the stirred reactor is a reactor equipped with a stirrer rotating at high speed to disperse the medium in the medium including hydrogen and fine bubbles as well as microorganisms to increase the access of microorganisms to the reagents.
- the stirred reactor has good production rates: values from 100 to 200
- the second function attributed to the carbonate-type material is the support function for the microorganisms responsible for the methanation (see claim 1: "a population of anaerobic methanogenic bacteria specifically adapted for the conversion of carbon dioxide to methane attached to the particulate ore carbonate in said bed ".).
- the water must be gradually evacuated to allow a continuous decomposition of the carbonate until exhaustion to provide the carbon necessary for methanation.
- This document relates to the production of synthetic methane by biological hydrogenation of CO2.
- This document proposes to use a support promoting the growth and densification of microorganisms in contrast to biological systems in which these same organisms are diluted in the aqueous phase.
- This document also discloses a water inlet and a dihydrogen inlet.
- this document proposes to use a carbonate-type carrier material to provide the CO2 required for biological methanation.
- This property implies decomposition of the carbonate during the production of synthetic methane. This requires renewal or regeneration to the system.
- the present invention aims to remedy all or part of these disadvantages.
- the present invention is directed to a biological methanation reactor for dihydrogen or a gas rich in dihydrogen and carbon dioxide or a gas rich in carbon dioxide with a fluidized bed, which comprises:
- the mobile support serves as a colonization site for microorganisms and by its surface / volume ratio it makes it possible to create a large contact area between the microorganisms and the medium. Moreover, by immobilizing the microorganisms on a support, one obtains a more important concentration effect of the biomass than in the case of the free cultures. These two effects combine to increase the reaction capacity per unit volume and thus reduce the footprint of the reactor. They also make it possible to obtain residuals that are very low in reagents in the product gas.
- This invention aims to implement the biological methanation within a fluidized layer of non-consumable material with introduction of carbon dioxide, dihydrogen and water (recirculation and removal of excess produced by the reaction).
- non-consumable it is meant that the material does not decompose during the production of synthetic methane, the material only serving as a support for the methanogenic flora but not participating directly in the reaction except for accommodating the population bacterial.
- an example of a consumable material is disclosed, for example, in US Patent Application 4,571,384.
- the cross sectional area of an interior volume of the enclosure is an increasing function along the longitudinal axis of the enclosure from the low end to the high end.
- the reactor that is the subject of the present invention comprises at least one water-collecting overflow positioned upstream of the methane or methane-rich gas outlet and the water outlet, oriented towards the upper end of the outlet.
- the enclosure forming a collector for the water passing over the overflow, the outlet for water being positioned in this manifold.
- the reactor that is the subject of the present invention comprises:
- At least one recirculation pump for the water passing through the water outlet of the enclosure
- At least one heat exchanger configured to heat or cool the water leaving the enclosure
- the recirculated water, at the outlet of the heat exchanger being at least partially reinjected into the chamber through an injection pipe.
- the reactor that is the subject of the present invention comprises means for measuring the water level in the enclosure and a water discharge from the reactor, the opening of the outlet being controlled according to the level of water measured water.
- this same means of measuring the level in the enclosure controls the opening of a water inlet when the level is too low.
- the recirculated water is injected into a stream comprising at least dihydrogen and / or carbon dioxide, upstream of the dihydrogen inlet and / or the carbon dioxide inlet into the stream. pregnant.
- the enclosure has an inlet for additional nutrients and / or reagents and / or water.
- the enclosure has a water outlet at the bottom of the enclosure.
- the additional nutrients and / or reagents are injected into the injection line in recirculated water.
- the entry for dihydrogen or for a gas rich in hydrogen, the entry for carbon dioxide or carbon dioxide rich gas and the primary water inlet are merged.
- the reactor that is the subject of the present invention comprises, upstream of the combined inlet of water, of hydrogen or of a gas rich in hydrogen and carbon dioxide or of a gas rich in carbon dioxide, a means of of dissolving carbon dioxide and dihydrogen in water.
- the recirculated water is injected at least in part into the dissolution means.
- the reactor that is the subject of the present invention comprises means for dissolving carbon dioxide in water on the one hand and means for dissolving dihydrogen in water on the other hand, each dissolution means being supplied with water by recirculated water, the recirculation rate of water to each dissolution means being controlled independently.
- FIG. 1 represents, schematically, a first particular embodiment of the device that is the subject of the present invention
- FIG. 2 represents, schematically, a second particular embodiment of the device that is the subject of the present invention
- FIG. 3 represents, schematically, a variant of the first particular embodiment of the device that is the subject of the present invention.
- FIG. 4 shows schematically a variant of the second particular embodiment of the device object of the present invention.
- FIG. 1 which is not to scale, shows a schematic view of one embodiment of the reactor 100 which is the subject of the present invention.
- This reactor 100 for biological methanation of hydrogen or a gas rich in hydrogen and carbon dioxide or a gas rich in carbon dioxide with a fluidized bed comprises:
- an enclosure 105 having a so-called “low” longitudinal end 107 and an opposite “high” opposite longitudinal end 106, said enclosure comprising, close to the low end:
- an output 1 for synthetic methane or for a gas rich in synthetic methane is an output 1 for synthetic methane or for a gas rich in synthetic methane
- a support material that can not be consumed by the methanation reaction to form a bed of methanogenic flora, having a density greater than the density of water, configured to receive a methanogenic flora.
- the enclosure 105 is, for example, formed of a closed and sealed volume having openings for positioning inputs or outputs of reagents, auxiliary reagents, nutrients, water or gas in the closed volume.
- This closed volume allows the constitution of a methanogenic medium for the methanation reaction to occur.
- the shape, internal and / or external, of the enclosure 105 is of no importance for the present invention as long as the enclosure is leakproof.
- the enclosure 105 has a tubular shape, that is to say a cylindrical shape, which can be oblong as shown in FIG.
- the cross sectional area of an interior volume 130 of the enclosure is an increasing function along the longitudinal axis of the enclosure 105 from the low end to the end. 106 high. This allows the inner volume 130 to have a flare limiting the capacity of the gas and water injected into the enclosure 105 to move the support material 125 beyond a height 101.
- This enclosure 105 has a low longitudinal end 107 intended to be positioned close to the ground of the positioning site of the reactor 100.
- This enclosure 105 has a high longitudinal end 106 intended to be positioned distally from the ground of the positioning site of the reactor 100.
- the enclosure 105 includes, near the low end:
- Each inlet 1 10 is, for example, an injection nozzle. However, any fluid injection member usually used in a biological methanation reactor or in a fluidized bed reactor can be used to make each inlet 1 10.
- Each input 1 10 in the enclosure 105 may be distinct.
- Each inlet, 10 is, for example, an injection nozzle, a nozzle, a perforated tube, a piping network equipped with strainers. However, any fluid injection member usually used in a biological methanation reactor can be used to make each inlet 1 10.
- At least two inputs 1 10 are combined.
- a means, 165 and / or 170, of dissolution of each gas whose input 1 10 is merged with the primary inlet 1 10 for water is positioned upstream of said confused inlet.
- the enclosure 105 includes, near the high end:
- Each outlet, 1 and 120 is, for example, an opening formed in the enclosure 105 connected to a transport pipe.
- the outlet 120 for water is located closer to the lower end 107 of the enclosure 105 than the outlet 15 for synthetic methane.
- the outlet 120 is equipped with a separation device for removing debris from the development of microorganisms (cyclone, filter for example).
- This device may be either upstream of the outlet, therefore in the reactor, or downstream of the outlet, thus outside the reactor.
- the reactor 100 comprises heat exchange tubes immersed in the chamber 105 and traversed by a fluid having a temperature compatible with the nominal operating temperature inside the chamber 105 during operation of the reactor
- the fluid may be at a higher temperature than the interior of the chamber to allow the reactor to be reheated or kept warm, or it may be colder than the interior of the enclosure to allow maintenance in reactor temperature by evacuating excess heat.
- the dihydrogen or the hydrogen-rich gas and the carbon dioxide or the carbon dioxide-rich gas move vertically in the enclosure 105, from the low end 107 towards the high end 106, and thus cross the support material 125 during this movement.
- the methanogenic flora transforms these reagents into methane, and the gaseous methane also moves towards the upper end 106 of the enclosure 105, forming a gaseous sky in the upper part of the enclosure 105. This gaseous sky is evacuated by the exit 1 15 for synthetic methane or gas rich in synthetic methane.
- the support material is, for example, composed of balls made of a denser material than water. These beads allow the accumulation of methanogenic flora, this flora being formed by the family of Archaea microorganisms for example.
- the beads are made, for example, of expanded clay, sand, alumina, crosslinked polymers such as copolymers of divinylbenzene and styrene or divinylbenzene and acrylic acid or methacrylate or weighted polymers.
- This support material 125 allows the development of a concentrated methanogenic flora at the support material 125, the support material 125 moving in the chamber 105 by the fluidization induced by the flow of gas and water.
- the fluidization is mainly induced by the formation of gas bubbles and by their coalescence during their ascent in the methanogenic layer.
- the fluidized bed reactor as disclosed above makes it possible to create a very large contact area and intense agitation between the microorganisms and the reactive gases without the need for a mechanical stirrer.
- this invention also makes it possible to overcome any risk of clogging of the bed by bacterial growth due to the permanent movement of the support material 125 by the fluidization phenomenon that can be likened to a perfectly mixed reaction medium.
- it is possible to work at high pressures without risk of gas leakage and without risk of failure of a sensitive mechanical element that constitutes a stirrer.
- the use of an agitator, to ensure good contact between the microorganisms and the reagents requires perfectly mastering the a crizlic system.
- the present invention simplifies the design of the biological methanation reactor.
- the reactor 100 comprises at least one water-collecting overflow 135 positioned upstream of the methane outlet 1 and the water-oriented exit 120.
- the upper end 106 of the enclosure 105 forming a collector for water passing over the overflow, the outlet 120 for water being positioned in this manifold.
- the overflow 135 may be a trough or channel or any other gravity water collection system.
- the overflow 135 is preferably positioned on the inner periphery of the enclosure 105 so as to follow at least part of the inside of the perimeter of the cross section of the enclosure 105. This overflow 135 makes it possible to collect the excess water in the enclosure 105.
- the reactor 100 comprises:
- At least one pump 140 for recirculating the water passing through the outlet 120 for water of the enclosure 105 and
- At least one heat exchanger 145 configured to heat or cool the water leaving the chamber
- Each pump is, for example, a centrifugal pump, piston, diaphragm, screw, gear or peristaltic.
- Each heat exchanger is, for example, tubular or plate type.
- the heat exchanger 145 is controlled, for example, as a function of a temperature value sensed inside the enclosure 105, at the level of the support material 125 for example or its outlet temperature.
- the reactor 100 comprises a temperature sensor (not shown) positioned inside the enclosure or in a pipe connecting the heat exchanger 145 and the primary outlet 120 for water.
- the exchangers can be positioned in parallel or in series according to the operating conditions desired by the reactor installer.
- the reactor 100 comprises an outlet 175 for water positioned upstream of the inlet 10 for water to evacuate recirculated water so as to regulate the water level. water in the enclosure and / or the flow of water entering the enclosure.
- the water injected into the reactor 100 is preheated or pre-cooled to a predetermined temperature, this temperature being able to depend on a temperature sensed by the temperature sensor of the reactor 100 described above.
- the injected water has a temperature adapted to maintain a temperature in the chamber, allowing the development of the flora.
- This temperature is, for example, between 30 and 70 ° C and preferably between 60 and 65 ° C.
- the water is injected, preferably, at the lowest possible temperature, above 0 ° C., which makes it possible to maintain the flora development temperature, given the operating conditions of the reactor.
- the recirculated water is supplied to the primary water inlet 120 through the injection line 150.
- the reactor 100 comprises a means 155 for measuring the water level in the enclosure and at least one water discharge 160 for the reactor, the opening of the reactor evacuation being controlled according to the measured water level and a set value.
- the evacuation 160 is open, which allows a final water outlet avoiding any recirculation related to the pump 140.
- the recirculated water is injected into a flow comprising at least dihydrogen and / or carbon dioxide, upstream of the inlet 1 for dihydrogen and / or the entry 1 10 for carbon dioxide in the enclosure.
- the enclosure 105 comprises at least one inlet 10 for additional nutrients and / or reagents and / or water.
- the reactor 300 comprises a water level sensor 305 in the enclosure 105.
- the exceeding of a predetermined predetermined water level causes the emission an opening command of a valve 310 for discharging water from the reactor 300.
- This valve 310 is connected, for example, to a dedicated water outlet 315 of the enclosure 105.
- a command is issued for water to be injected into the enclosure 105.
- the emission of these commands can be achieved by the sensor 305, by an associated electronic level sensor (not shown) or by an electronic control circuit (not shown) of the reactor 300 for example.
- the nutrients promote the development of the methanogenic flora while the additional reagents are intended to limit certain inconveniences in the reaction medium inside the enclosure 105.
- additional reagents include, for example, pH regulators or anti-foams. .
- the inlet 165 is coincident with at least one of the entries for water 1 10, for dihydrogen and / or for carbon dioxide,
- the injection of nutrients into the reaction chamber may be carried out at predetermined times after activation of the reactor 100, for example.
- the injection of additional reagents can be carried out as a function of the capture of values of physical quantities inside the enclosure 105.
- the injection of a pH regulating reagent can be controlled according to a pH value measured inside the enclosure 105 or the water passing through the primary outlet 120 for water.
- the additional nutrients and / or reagents are injected into the recirculated water injection line 150.
- the reactor 100 comprises, upstream of the inlet 1, which is a mixture of water, hydrogen and carbon dioxide, a means, 165 or 170, for dissolving the carbon dioxide and dihydrogen in water. Nutrients and / or reagents and / or make-up water may be injected into this dissolution means, 165 and / or 170.
- Each dissolution means 165 and 170 is, for example, a packed column, a spray column, a bubble column or any other dissolution device for dissolving a gas in a liquid.
- each means, 165 and 170, of dissolution can be common to both a carbon dioxide inlet and a dihydrogen inlet, these arrivals possibly being confused.
- the reactor 100 comprises means 165 and 170 for dissolving separately for carbon dioxide on the one hand and for dihydrogen on the other hand.
- the recirculated water is injected at least in part into the dissolution means 165 and 170 if the reactor 100 comprises only one such means 165 or 170 for dissolving.
- the supply of recirculated water by means of, 165 or 170, dissolution depends for example on a level of water captured in the means, 165 or 170, dissolution or a flow of gas entering the means, 165 or 170, of dissolution.
- each means, 165 and 170 can be supplied with recirculated water from a same primary outlet 120 for water or separate outputs, l recirculated water being distributed between the dissolution means 165 and 170 and possibly a direct injection pipe in the enclosure bypassing each dissolution means.
- the reactor 100 comprises at least two primary water outlets 120 and, for each outlet 120, at least one pump 140 and at least one heat exchanger 145.
- Recirculated water by a first pump 140 is injected either into a first means 165 for dissolving carbon dioxide in the water, or directly in the enclosure 105.
- the water recirculated by a second pump 140 is injected either into a second means 170 of dissolution of dihydrogen in water, either directly in the enclosure 105.
- each flow rate is controlled independently.
- Each flow rate is controlled, for example, as a function of the flow of gas entering the means, 165 and 170, dissolution and a total flow setpoint value to have a correct fluidization of the support bed.
- FIG. 2 which is not to scale, shows a schematic view of one embodiment of the reactor 200 which is the subject of the present invention.
- This reactor 200 for biological methanation of dihydrogen and of fluidized bed carbon dioxide comprises:
- an enclosure 105 having a so-called “low” longitudinal end 107 and an opposite “high” opposite longitudinal end 106, said enclosure comprising, close to the low end: a primary water inlet
- a non-consumable support material 125 for forming a bed of methanogenic flora having a density greater than the density of water, configured to receive a methanogenic flora.
- FIG. 2 shows, in particular, a reactor 200 identical to the reactor 100 as described with reference to FIG. 1, which further comprises at least one bypass of at least one of: a heat exchanger 145 and or a means, 165 or 170, of dissolution.
- the reactor 400 comprises a water level sensor 405 in the enclosure 105.
- the exceeding of a predetermined predetermined water level causes the emission an opening command of a valve 410 for discharging water from the reactor 400.
- This valve 410 is connected, for example, to a dedicated water outlet 415 of the enclosure 105.
- the emission of these commands can be achieved by the sensor 405, by an associated electronic level sensor (not shown) or by an electronic control circuit (not shown) of the reactor 400 for example.
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Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP18769754.5A EP3668964A1 (fr) | 2017-08-16 | 2018-08-09 | Réacteur de méthanation biologique |
BR112020003154-2A BR112020003154B1 (pt) | 2017-08-16 | 2018-08-09 | Reator de metanação biológica |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1757705 | 2017-08-16 | ||
FR1757705A FR3070166B1 (fr) | 2017-08-16 | 2017-08-16 | Reacteur de methanation biologique |
Publications (1)
Publication Number | Publication Date |
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WO2019034819A1 true WO2019034819A1 (fr) | 2019-02-21 |
Family
ID=60923584
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2018/052038 WO2019034819A1 (fr) | 2017-08-16 | 2018-08-09 | Réacteur de méthanation biologique |
Country Status (3)
Country | Link |
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EP (1) | EP3668964A1 (fr) |
FR (1) | FR3070166B1 (fr) |
WO (1) | WO2019034819A1 (fr) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2021234073A1 (fr) | 2020-05-20 | 2021-11-25 | Tma-Process | Procede de methanation de l'hydrogene h2 et du dioxyde de carbone co2 ou de l'hydrogene h2 et du monoxyde de carbone co en vue de la production de methane ch4 |
LU501102B1 (fr) * | 2021-12-28 | 2023-06-28 | Luxembourg Inst Science & Tech List | Reacteur de methanation biologique exploitant une flore microbienne en suspension et procede de mise en oeuvre d’un tel reacteur |
FR3141697A1 (fr) * | 2022-11-07 | 2024-05-10 | Universite Clermont Auvergne | Procede de biomethanation ex-situ |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4322296A (en) * | 1980-08-12 | 1982-03-30 | Kansas State Univ. Research Foundation | Method for wastewater treatment in fluidized bed biological reactors |
US4571384A (en) | 1982-10-18 | 1986-02-18 | State Of Oregon Acting By And Through The State Board Of Higher Education On Behalf Of Oregon State University | Methane production |
EP1574581A2 (fr) * | 2004-03-08 | 2005-09-14 | E.M. Engineering F.T.S. B.V. | Méthode et appareil pour la preparation de méthane |
DE102011051836A1 (de) | 2010-07-15 | 2012-01-19 | Brandenburgische Technische Universität Cottbus | Verfahren und Vorrichtung zur Nutzung gasförmiger Substrate für die Gewinnung von Biogas |
-
2017
- 2017-08-16 FR FR1757705A patent/FR3070166B1/fr active Active
-
2018
- 2018-08-09 WO PCT/FR2018/052038 patent/WO2019034819A1/fr unknown
- 2018-08-09 EP EP18769754.5A patent/EP3668964A1/fr active Pending
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4322296A (en) * | 1980-08-12 | 1982-03-30 | Kansas State Univ. Research Foundation | Method for wastewater treatment in fluidized bed biological reactors |
US4571384A (en) | 1982-10-18 | 1986-02-18 | State Of Oregon Acting By And Through The State Board Of Higher Education On Behalf Of Oregon State University | Methane production |
EP1574581A2 (fr) * | 2004-03-08 | 2005-09-14 | E.M. Engineering F.T.S. B.V. | Méthode et appareil pour la preparation de méthane |
DE102011051836A1 (de) | 2010-07-15 | 2012-01-19 | Brandenburgische Technische Universität Cottbus | Verfahren und Vorrichtung zur Nutzung gasförmiger Substrate für die Gewinnung von Biogas |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2021234073A1 (fr) | 2020-05-20 | 2021-11-25 | Tma-Process | Procede de methanation de l'hydrogene h2 et du dioxyde de carbone co2 ou de l'hydrogene h2 et du monoxyde de carbone co en vue de la production de methane ch4 |
FR3110601A1 (fr) | 2020-05-20 | 2021-11-26 | Tma-Process | Procédé de méthanation de l’hydrogène H2et du dioxyde de carbone CO2ou de l’hydrogène H2et du monoxyde de carbone CO en vue de la production de méthane CH4 |
LU501102B1 (fr) * | 2021-12-28 | 2023-06-28 | Luxembourg Inst Science & Tech List | Reacteur de methanation biologique exploitant une flore microbienne en suspension et procede de mise en oeuvre d’un tel reacteur |
WO2023126177A1 (fr) * | 2021-12-28 | 2023-07-06 | Luxembourg Institute Of Science And Technology | Réacteur de méthanation biologique utilisant une flore microbienne en suspension et procédé d'utilisation d'un tel réacteur |
FR3141697A1 (fr) * | 2022-11-07 | 2024-05-10 | Universite Clermont Auvergne | Procede de biomethanation ex-situ |
WO2024099984A1 (fr) * | 2022-11-07 | 2024-05-16 | Universite Clermont Auvergne | Procede de biomethanation ex-situ |
Also Published As
Publication number | Publication date |
---|---|
BR112020003154A2 (pt) | 2020-09-15 |
FR3070166A1 (fr) | 2019-02-22 |
EP3668964A1 (fr) | 2020-06-24 |
FR3070166B1 (fr) | 2021-01-29 |
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