EP2652117A2 - Procédé et installation pour la méthanisation de la biomasse - Google Patents

Procédé et installation pour la méthanisation de la biomasse

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Publication number
EP2652117A2
EP2652117A2 EP11796629.1A EP11796629A EP2652117A2 EP 2652117 A2 EP2652117 A2 EP 2652117A2 EP 11796629 A EP11796629 A EP 11796629A EP 2652117 A2 EP2652117 A2 EP 2652117A2
Authority
EP
European Patent Office
Prior art keywords
gas
storage unit
gas storage
fermenter
methane
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP11796629.1A
Other languages
German (de)
English (en)
Inventor
Carsten Hempel
Oliver Jaroschek
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Schmack Biogas GmbH
Original Assignee
Schmack Biogas GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Schmack Biogas GmbH filed Critical Schmack Biogas GmbH
Publication of EP2652117A2 publication Critical patent/EP2652117A2/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
    • C12P5/02—Preparation of hydrocarbons or halogenated hydrocarbons acyclic
    • C12P5/023—Methane
    • 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
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/24—Gas permeable parts
    • 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
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/36—Means for collection or storage of gas; Gas holders
    • 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
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/02—Percolation
    • 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 method for methanization of biomass and energetic utilization of the biogas obtained in a device having at least one batch fermenter. It furthermore relates to a plant suitable for carrying out such a process for the methanization of biomass and the energetic utilization of the biogas obtained.
  • a plant type which is preferred for various boundary conditions is oriented towards the discontinuous, batch-type fermentation of pourable substrate with a relatively high dry matter content.
  • a comparatively high degree of flexibility with regard to the biomass to be methanized, ie the starting material, and a - even with rather inhomogeneous starting material - well controlled process control For example, DE 10257849 A1, DE 19719323 A1, DE 10050623 B4, EP 934998 B1, DE 10034279 A1, WO 02/06439 A2, EP1681274 A2, DE 102008015240 A1 and EP 1997875 A1 belong to the relevant prior art with regard to this type of installation ,
  • US Pat. No. 4,111,429 B2 also discloses a process of the type mentioned at the beginning for the methanation of biomass and a plant suitable for carrying out the process in question.
  • the latter preferably comprises a plurality of fermenters, which are operated out of phase with one another in a two- or three-stage process for the decomposition of organic substance.
  • the (anaerobic) methanization phase is preceded by a rotting phase in which the biomass is aerobically composted to form essentially CO 2 , the heat produced thereby heating the biomass and thereby promoting the subsequent fermentation.
  • further composting takes place, for which purpose the fermented substrate is aerated.
  • the individual fermenters of the plant are connected to each other, for example, to a fermenter - to stimulate the fermentation - with the one another, out-of-phase fermenter removed to inoculate leachate or to heat the biomass in another fermenter with the warm exhaust air from a fermenter operating in the aerobic phase in order to stimulate ethanization there.
  • the present invention has set itself the task of providing a particularly economical and at the same time environmentally sound method for methanating biomass and energetic utilization of the biogas obtained in a device having at least one batch fermenter and a plant suitable for carrying out the process in question.
  • the comparatively methane-poor gas mixture which leaves the fermenter during the rinsing phase and, taken by itself, has a low methane concentration counteracting economic energy recovery can be utilized in the facility which is available for the energy recovery of the "normal", ie methane-rich biogas which purpose it is initially collected in the second gas storage unit separated from methane-rich biogas formed in the fermentation phase and energetically utilized at a later time, wherein the gas taken from the second gas storage unit for the purpose of energy recovery with methane-rich biogas, which is taken at the same time the first gas storage unit, is mixed to an energetically used mixed gas.
  • the "normal" ie methane-rich biogas which purpose it is initially collected in the second gas storage unit separated from methane-rich biogas formed in the fermentation phase and energetically utilized at a later time
  • the proportion of energetically used biogas can be increased, which is beneficial for economic efficiency and, at the same time, because correspondingly less gas is released to the environment via a torch, a filter or another device. ben, which increases environmental compatibility. It is also advantageous for the economy that, in application of the present invention, the duration of the rinsing phase can be shortened significantly compared with the prior art, which, in other words, due to the reduced unproductive time
  • a likewise preferred form of energetic utilization of the biogas produced using the method according to the invention consists in its feeding into a natural gas network, in which case the gas transfer station or
  • Gas supply system is the device for the energetic utilization of biogas in the sense of the existing terminology.
  • the prerequisite for the gas feed is the achievement of the quality of natural gas, so that the biogas produced must still be treated prior to feeding with the biogas upgrading methods known from the prior art (eg desulfurization, drying, CO 2 removal).
  • both the first gas storage unit and the second gas storage unit serve solely to temporarily store gas taken from the fermenter (s) to subsequently energize the gas stored in the second gas storage unit by admixture with the first gas storage unit Gas storage unit to allow extracted gas.
  • the fermenters themselves therefore do not constitute gas storage units in the sense of the present invention.
  • the plant according to the invention for the methanization of biomass and energetic utilization of the biogas obtained comprises at least one airtight sealable feed opening, at least one gas outlet and a purge air inlet fermenter, at least one scavenge air blower , a first gas storage unit, a second gas storage unit, a gas line network connecting the at least one fermenter to the first and second gas storage unit, a gas control valve, a biogas energy recovery device, and a system control adjusting the gas control valves, the gas control valves the system control are adjustable so that with the at least one gas outlet either the first gas storage unit or the second gas storage unit and that optionally only the first e gas storage unit or at the same time both the first and the second gas storage unit with the means for energetic utilization of biogas are fluidically connectable.
  • the gas mixture leaving the fermenter can be fed into the first gas storage unit.
  • the gas mixture leaving the fermenter through the gas outlet often still has a relatively high methane concentration (eg a CH 4 content between 20% and 48%) under typical boundary conditions, so that it is comparable in terms of usability during the
  • Fermentation phase obtained methane-rich biogas. And even in the case of a significantly lower methane content (down to about 20%) affects - because of the resulting typical methanation processes proportions of the methane-rich biogas obtained during the fermentation phase and the gas mixture generated during purging of the fermenter with purging air, the feed of the fermenter in the first period of the rinsing phase through the gas outlet leaving still relatively methane-rich gas mixture (CH 4 - content, for example> 20%) in the first gas storage unit not adversely affect the usability of the methane-rich biogas stored there.
  • CH 4 - content for example> 20%
  • the fermenter leaving, very methane-poor gas mixture (CH 4 content, for example, ⁇ 4%) via a biofilter during a final period of purging given the environment.
  • CH 4 content for example, ⁇ 4%
  • the energetic usability of the gas stored there is obtained.
  • Generating biogas or a gas mixture that is located in the lower part of the chess gas eg CH 4 content between 4% and 10%
  • the installation intended to carry out the process in question is typically equipped with a device for monitoring the quality (ie the methane content) of the equipped respective fermenter leaving gas, the device in question acts on the plant control, so that the latter can operate the gas control valves in dependence on the respective gas quality.
  • the device in question acts on the plant control, so that the latter can operate the gas control valves in dependence on the respective gas quality.
  • a pure time control is considered, in which case empirical values of the duration of the individual phases and phase sections within the cycle 1 are utilized in the corresponding time programming of the system control ,
  • the formation and energetic utilization of the mixed gas preferably takes place intermittently.
  • the formation and energetic utilization of the mixed gas takes place during the biomass change (steps f and a) and the first period of the subsequent fermentation phase (start-fermentation phase), wherein the energetic utilization of the mixed gas can possibly also be initiated towards the end of the rinsing phase.
  • start-fermentation phase the first period of the subsequent fermentation phase
  • the second gas storage unit is driven substantially empty during the start-fermentation phase.
  • a biogas with a methane concentration that is so high may, if appropriate, also be formed in the start-up fermentation phase in such a way that feeding the biogas into the first gas storage unit that is leaving the fermenter in this phase is expedient.
  • the phases of feeding the relatively low-methane gas mixture in the second gas storage unit during the purging phase are substantially shorter than the phases of removal of gas from the second gas storage unit for its energy recovery.
  • the energy recovery of the gas stored in the second gas storage unit is typically extended over a longer period of time compared to the duration of feeding the relatively low-methane gas mixture into the second gas storage unit during the purge phase.
  • the rinsing process is made comparatively short in terms of high productivity. that can.
  • the flushing process of typically sized fermenters eg 1,000 m 3
  • a further particularly preferred embodiment of the present invention is characterized in that the duration of the rinsing phase only about 0.2 to 1.0%, more preferably even only about 0.3 to 0.8% of the total cycle time is.
  • the particularly short rinsing phase possible in application of the present invention can also be expressed by the fact that the gas exchange rate during rinsing of the fermenter with rinsing air is preferably between 1 / h and 10 / h , Particularly preferably between 2 / h and 6 / h, based on the volume of gas in the fermenter chamber.
  • methane concentration in the second gas storage unit by feeding methane-rich biogas is always above the value of 16.5% and thus above the upper explosive limit for methane in air is held.
  • Perkolatfermenter is deducted. Exactly that of the percolate fermenter withdrawn methane-rich biogas is thus fed in this embodiment of the invention in the second gas storage unit, namely, as stated, as a template gas before the methane-poor gas mixture is fed from the rinsing phase in the second gas storage unit.
  • methane-rich biogas discharged from a percolate fermenter be fed into the second gas storage unit as said template gas.
  • methane-rich biogas which is formed in the fermenter in the fermentation phase, is fundamentally also suitable for this purpose.
  • the feeding of methane-rich biogas into the second gas storage unit can in particular also be carried out from the fermenter during the fermentation phase. It is also conceivable that for enrichment tion of the gas stored in the second gas storage unit of the first gas storage unit methane-rich biogas and is fed into the second gas storage unit.
  • the process of the invention is by no means dependent on (methane-rich) biogas formed in a percolate fermenter, so that it can accordingly also run in plants that have no percolate fermenter or in which the biogas formed in a percolate fermenter is otherwise used.
  • Rinsing in this case should by no means only be understood to mean the replacement of the gas existing over the fermentation substrate by air. Rinsing also involves actively stopping the remaining methane formation by removing the (anaerobic)
  • Methane-forming bacteria are exposed to an aerobic atmosphere, wherein even during the rinsing process, a certain amount of methane is newly formed.
  • the rinse is quite a part of the biological processes.
  • this process section can be accelerated due to the specific treatment of the gas mixture leaving the fermenter during the rinsing phase, and the duration of the rinsing phase can thereby be shortened.
  • the gas line network for each fermenter can certainly also include two gas lines, wherein biogas is fed through one of the two gas lines of the first gas storage unit and gas through the other gas line of the second gas storage unit and each of the two gas lines at a separate opening connected to the fermenter in question.
  • biogas is fed through one of the two gas lines of the first gas storage unit and gas through the other gas line of the second gas storage unit and each of the two gas lines at a separate opening connected to the fermenter in question.
  • the gas pipeline network can also comprise a connecting line connecting the two gas storage units with one another, by means of which is passed through if necessary methane-rich biogas from the first gas storage unit in the second gas storage unit to enrich the gas stored there (see above).
  • shut-off valves are expediently proportional valves, which between the complete
  • the fully closed position can take any intermediate positions in order to set the respective flow as desired.
  • the plant is operated in accordance with the invention depends on various current and plant-specific parameters and in particular the individual biomass.
  • the type of device for energy recovery of the biogas obtained determines with which methane gas biogas can be utilized, it should be noted in view of the above values that future technological developments, for example, the combustion of biogas in a combined heat and power plant even at methane concentrations of significantly less than 48% is conceivable.
  • the volume of the fermenter, the substrate level and the scavenging air blower typically determine which volume of gas mixture is formed with which methane concentration during the rinsing process.
  • Fig. 1 shows a schematic representation of a plant comprising three fermenters for the methanation of biomass and energetic utilization of the biogas obtained according to the present invention
  • the system shown in FIG. 1 for the methanation of biomass and energetic utilization of the biogas obtained comprises three identically constructed, rack-shaped fermenters 1.
  • Each of the fermenters 1 has an airtight sealable feed opening 2, a first gas outlet 3, a second gas outlet 4 and a with a corresponding scavenging air fan 5 in connection scavenging air inlet 6.
  • the plant is equipped with a percolate system, which is a percolate container 7, which also represents a Perkolatfermenter 8, and a Includes percolate cycle.
  • the percolate cycle in this case has percolate lines 9, pumps 10 and 11 and each fermenter 1 a - each controllable via a lockable valve 43 - irrigation strand 12 and a gutter 13.
  • two gas storage units are provided, namely a first gas storage unit 14 and a second gas storage unit 15, each of which comprises at least one gas storage of conventional design.
  • the fermenters 1 are connected to the two gas storage units 14 and 15 via a gas line network 16.
  • This comprises a first gas line 17 and a second gas line 18, the first gas line 17 (correspondingly branched), the first gas storage unit 14 each via a lockable valve 19 with the
  • a controllable directional control valve 21 is provided, by means of which the fermenter 1 or gas leaving via the respective second gas outlet 4 can optionally be supplied to an advancing gas system 22 instead of the second gas storage unit 15.
  • the fortification system 22 comprises a biofilm ter 23 and a gas torch 24, which can optionally be - applied via another controllable directional control valve 25.
  • the first gas storage unit 14 and the second gas storage unit 15 are connected to each other by means of a connecting line 26, in which a lockable valve 27 is arranged, wherein in the connecting line 26, if necessary, a - not shown - blower or a compressor may be provided to Biogas from the first gas storage unit 14 in the second gas storage unit 15 to promote. Furthermore, the connecting line 26, if necessary, a - not shown - blower or a compressor may be provided to Biogas from the first gas storage unit 14 in the second gas storage unit 15 to promote. Furthermore, the connecting line 26, if necessary, a - not shown - blower or a compressor may be provided to Biogas from the first gas storage unit 14 in the second gas storage unit 15 to promote. Furthermore, the connecting line 26, in which a lockable valve 27 is arranged, wherein in the connecting line 26, if necessary, a - not shown - blower or a compressor may be provided to Biogas from the first gas storage unit 14 in the second gas storage unit 15 to promote. Furthermore, the connecting line 26,
  • Perkolatfermenter 8 connected via a (correspondingly branched) gas line 28 with both the first gas storage unit 14 and the second gas storage unit 15, wherein in each of the two strands a lockable valve 29 and 30 is arranged.
  • the energy utilization of the recovered biogas serving device 31 includes a cogeneration unit 32, which is connected to a Nutzgas-line network 33, which forms part of the gas line network 16, both with the first gas storage unit 14 and with the second gas storage unit 15.
  • a gas mixer 34 is arranged in which a first useful gas line 36 connected to the first gas storage unit 14 via a lockable valve 35 and a second gas storage unit 15 via a lockable valve 37
  • All controllable and lockable valves and the pumps 10 and 11, the flushing fan 5 and the cogeneration unit 32 are controllable by means of the system controller 40.
  • the system controller 40 also utilizes current operating data of the combined heat and power plant 32, and in particular the measurement data provided by sensors 41 and 42 for the methane content of the gas present in the first gas storage unit 14 or the second gas storage unit, the latter in particular with regard to the above
  • the Plant control 40 different further, for example, in the gas lines 17, 18 and 28 determined measurements of gas qualities and flow rates are taken into account.
  • the operating cycle is roughly subdivided into four phases, namely feeding the fermenter with biomass (section I), fermentation phase (section II), rinsing phase (section III) and discharge phase (section IV).
  • the indicated positions of the various valves show, on the one hand, the phase-wise changing charge of the two gas storage units 14 and 15 from the respective fermenter 1 and the percolate fermenter 8 and, on the other hand, also the phase-wise alternating removal of gas from the two gas storage units 14 and 15 for the purpose of energy recovery in the Block CHP 32 on.
  • both gas outlets 3 and 4 are closed by means of the associated valves 19 and 20.
  • a mixed gas (methane content approximately between 48% and 60%) is burned in the combined heat and power plant 32, which is in the Gasmi 34 is formed by mixing gas extracted from the first gas storage unit 14 (via the opened valve 35) and the second gas storage unit 15 (via the opened valve 37).
  • the percolate fermenter 8 feeds methane-rich biogas into the first gas storage unit 14 in this phase (via the opened valve 29).
  • phase II During a more or less extensive first stage of the fermentation phase (Phase II), very low methane, initially still residual air containing gas in the fermenter 1 (via the appropriately controlled valves 20 and 21) first to the biofilter 23 and then (after reversing the valve 21) relatively low-methane biogas in the second gas storage unit 15 are fed. In this period (start-fermentation phase) mixed gas is still burned in the cogeneration unit 32. The percolate fermenter continues to feed methane-rich biogas into the first gas storage unit 14 during this period.
  • methane-rich biogas produced in the fermenter 1 (via the open valve 19 with the valve 20 closed) is fed into the first gas storage unit 14.
  • mixed gas is further burned in the combined heat and power plant 32 until such time as the second gas storage unit 15 is empty, before subsequently excluding the first gas storage unit 14
  • the valves 29 and 30 are reversed (at the same time), so that methane-rich biogas from the percolate fermenter 8 is fed into the second gas storage unit 15, alternatively or additionally also methane-rich biogas from the first gas storage unit 14 into the second gas storage unit 15 can be fed, with open valve 27 through the connecting line 26 therethrough.
  • the fermenter 1 leaving, typically still relatively rich in methane gas mixture, depending on the specific parameters to applicable gas quantity and quality, in the first gas storage unit 14 or abe the second gas storage unit 15 are fed.
  • the fermenter 1 leaving relatively methane-poor gas mixture is fed into the second gas storage unit 15.
  • biogas which has been removed from the first gas storage unit 14 is also burned in the cogeneration plant.
  • the duration of the continued supply of methane-rich template gas into the second gas storage unit 15 from the percolate fermenter 8 (via the opened valve 30) and / or the first gas storage unit 14 (via the opened valve 27) z the beginning of the rinsing phase depends on the estimated Demand for methane-rich biogas in order to maintain the methane content of the gas in the second gas storage unit 15 always above the upper explosion limit.
  • valves 29 and 30 are reversed again, so that from there on methane-rich biogas from the percolate fermenter 8 is fed back into the first gas storage unit 14. Also during this phase, the first gas storage unit 14 further biogas is burned in the combined heat and power plant.
  • the very methane-poor gas mixture leaving the fermenter 1 (with a methane content below the lower explosion limit) is discharged to the environment via the biofilter 23, for which purpose the valve 21
  • Gas mixer 34 is formed by mixing gas extracted from the first gas storage unit 14 and the second gas storage unit 15 extracted gas.

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Abstract

L'invention concerne un procédé pour la méthanisation de la biomasse et la valorisation énergétique du biogaz produit dans un dispositif comportant au moins un fermenteur (1) fonctionnant en procédé discontinu, caractérisé en ce que le fermenteur (1) est rempli de biomasse, l'ouverture de chargement (2) est fermée hermétiquement, un biogaz riche en méthane produit dans une phase de fermentation est introduit au moins temporairement dans une première unité de stockage de gaz (14), un mélange gazeux pauvre en méthane est introduit au moins temporairement dans une deuxième unité de stockage de gaz (15) pendant le rinçage du fermenteur (1) avec de l'air de rinçage, l'ouverture de chargement (2) est ouverte et le résidu de fermentation est éliminé du fermenteur (1). La valorisation énergétique du gaz stocké dans la deuxième unité de stockage de gaz (15) s'effectue de telle sorte que le gaz extrait de cette unité de stockage de gaz est mélangé avec le biogaz extrait de la première unité de stockage de gaz (14), avant que le gaz de mélange ainsi produit ne soit ensuite valorisé sur le plan énergétique.
EP11796629.1A 2010-12-15 2011-12-10 Procédé et installation pour la méthanisation de la biomasse Withdrawn EP2652117A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102010054676A DE102010054676A1 (de) 2010-12-15 2010-12-15 Verfahren und Anlage zur Methanisierung von Biomasse
PCT/EP2011/006238 WO2012079735A2 (fr) 2010-12-15 2011-12-10 Procédé et installation pour la méthanisation de la biomasse

Publications (1)

Publication Number Publication Date
EP2652117A2 true EP2652117A2 (fr) 2013-10-23

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Family Applications (1)

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EP11796629.1A Withdrawn EP2652117A2 (fr) 2010-12-15 2011-12-10 Procédé et installation pour la méthanisation de la biomasse

Country Status (5)

Country Link
US (1) US20130280779A1 (fr)
EP (1) EP2652117A2 (fr)
CA (1) CA2822247A1 (fr)
DE (1) DE102010054676A1 (fr)
WO (1) WO2012079735A2 (fr)

Families Citing this family (4)

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Publication number Priority date Publication date Assignee Title
EP2634257B1 (fr) * 2012-02-29 2018-09-26 Kompoferm GmbH Procédé de fermentation de biomasse
DE102013107683B4 (de) * 2013-07-18 2017-10-12 Peter Lutz Biogasanlage zur Erzeugung von Biogas aus nicht-pumpbarer Biomasse sowie Verfahren zu ihrem Betrieb
DE102013107754A1 (de) * 2013-07-19 2015-01-22 Peter Lutz Biogas-Anlage sowie Verfahren zu ihrem Betrieb
IT201800020656A1 (it) * 2018-12-21 2020-06-21 Hysytech Srl Impianto per la produzione di biometano e metodo di funzionamento dello stesso

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DE102010054676A1 (de) 2012-06-21
US20130280779A1 (en) 2013-10-24

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