WO2010110773A1 - Réacteur méthanogène - Google Patents

Réacteur méthanogène Download PDF

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Publication number
WO2010110773A1
WO2010110773A1 PCT/US2009/001896 US2009001896W WO2010110773A1 WO 2010110773 A1 WO2010110773 A1 WO 2010110773A1 US 2009001896 W US2009001896 W US 2009001896W WO 2010110773 A1 WO2010110773 A1 WO 2010110773A1
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WO
WIPO (PCT)
Prior art keywords
reactor vessel
interior space
operationally coupled
sparger
culture
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.)
Ceased
Application number
PCT/US2009/001896
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English (en)
Inventor
Bruce Schroder
Russell Pohl
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.)
Tech V LLC
Original Assignee
Tech V LLC
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 Tech V LLC filed Critical Tech V LLC
Priority to PCT/US2009/001896 priority Critical patent/WO2010110773A1/fr
Publication of WO2010110773A1 publication Critical patent/WO2010110773A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • 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
    • C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
    • 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
    • C12M29/18—External loop; Means for reintroduction of fermented biomass or liquid percolate
    • 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
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • C12M41/26—Means for regulation, monitoring, measurement or control, e.g. flow regulation of pH
    • 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
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • C12M41/28—Means for regulation, monitoring, measurement or control, e.g. flow regulation of redox potential
    • 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 the generation of green natural gas through methanogenic conversion and more particularly pertains to a new methanogenic reactor for generating natural gas and cellular biomass from a variety of input material including syngas, mixed gas, or combined individual gas streams.
  • Illustrative examples of the types of systems known in the prior art include anaerobic digestion systems and U. S . Patent Nos. 1 ,940,944; 2,097,454; 3 ,640,846 ; 4, 722 , 74 1 ; 5 ,82 1 , 1 1 1 and application no . PCT/US07/71 1 38.
  • the methanogenic reactor according to the present invention substantially departs from the conventional concepts and designs of the prior art, and in so doing provides an apparatus primarily developed for the purpose of generating green natural gas and cellular biomass from a variety of source materials.
  • Pelletizing improves the handling characteristics of biomass, but adds enough cost to the resulting fuel cost to largely eliminate any fuel cost advantage.
  • biomass fuels burn dirty, producing sulfur and nitrogen oxides and hydrogen chloride. Equipment to burn these fuels is expensive and air permitting remains problematic.
  • a clean solution to these limitations would be to convert biomass into pipeline quality biomethane near the point of origin for transmission to existing natural gas customers via existing natural gas pipelines.
  • Thi s same process can also supply biomethane to specialty chemical facilities for the production of green specialty chemi cals, including but not limited to "green plastics".
  • the present invention also generates cellular biomass, which may be utilized as a food or nutrient for livestock and humans
  • the three primary structures in a plant are cellulose, hemicelluloses, and lignin. These compounds are in turn polymers of 6-carbon sugars, 5-carbon sugars, and phenolics respectively. As the plant matures, there is a progressive conversion of cellulose and hemicelluloses to lignin. This is reflected in the decrease of total digestable nutrients and the increase of acid detergent fiber content.
  • Anaerobic digestion uses mixed cultures of microbes to break down biomass into fermentable sugars, amino acids, and organic acids. This process is multi-step and is subject to upset by overproduction of organic acids which kill the methanogenic organisims.
  • the great benefit of anaerobic digestion is that it is generally recognized as specific, producing methane and carbon dioxide in a readily recoverable form.
  • a further disadvantage of anaerobic digestion of grasses is that when native or prairie grass is cut before October, the yield the following year is half or less of what is expected. This appears to be related to the manner in which nutrients are returned to the root structure after frost.
  • Enzymatic processes to break down biomass to fermentable sugars remain an elusive and expensive undertaking. Even if successful, however, enzymatic processes are likely to be highly specific to certain species and perhaps even varieties within species due to their high specificity .
  • One of the obj ectives associated with biomass production is promotion of multiple species cultivation. Highly specific enzyme processes will tend to promote monocultures and leave the ecosystem no richer than a corn/soybean mix.
  • the present invention provides each of these advantages by using a hybrid process which combines the flexibility and power of gasification with the specificity of anaerobic digestion, and with improved efficiency and higher production rates than anaerobic digestion.
  • the gasification step overcomes biomass species and variety variations producing uniform, readily fermentable feedstock to the methanogenic reactor.
  • the culture in the methanogenic reactor is efficient and specific producing only methane, cellular biomass, and water as its co-products.
  • the present invention utilizes gases which maybe derived from a wide variety of feedstocks ranging from crop residues, low value co-products from agriculture processing and energy crops such as switchgrass and corn stover, waste wood products, and other similar biomass sources.
  • the raw materials may be processed such as being reduced to a uniform size and moisture content (preferably very low) prior to gasification.
  • the gassification process converts the biomass into an intermediate gas stream known as syngas or synthesis gas.
  • the syngas after going through a heat recovery process, may be directed through a filtering system and or a water gas shift prior to being directed into the methanogenic reactor vessel for conversion by the methanogenic culture into methane. It is important to note that while the present invention is directed towards providing green natural gas from biomass, the same process can be done with municipal or landfill wastes or nonconventional carbon and hydrogen sources ( collectively
  • landfill waste The use of the present invention with landfill wastes as the feed stock would allow the reclamation of hundreds of thousands of acres currently used as landfills. If landfill wastes are utilized as a feedstock, the filtering and cleanup process after gasification can be much more complex than that required for biomass feedstock.
  • the present invention can be utilized for the generation of cellular biomass.
  • Typical algae systems used for biomass generation produce between 0.2 and 4.0 grams per liter of reactor volume per day.
  • Other methanogenic systems have been reported to produce up to 2.88 grams per liter of reactor volume per day.
  • the present methanogenic reactor when properly operated in a biomass production mode, can produce 12 grams per liter of reactor volume per hour. This present approximately a 1 00Ox improvement over algae generation systems currently in use .
  • Figure 1 is a schematic functional block diagram of a new Methanogenic Reactor in use according to the present invention.
  • Figure 2 is a schematic functional block diagram of an embodiment of the present invention.
  • Figure 3 is a schematic functional block diagram of another embodiment of the present invention.
  • Figure 4 is a schematic functional block diagram of a further embodiment of the present invention.
  • Figure 5 is a schematic functional block diagram of still a further embodiment of the present invention.
  • Figure 6 is a schematic flow diagram of the present invention.
  • the methanogenic reactor 10 generally comprises a reactor vessel 1 1 for the methanogenic conversion of an input material stream to an output materials stream, including a bottom wall 21 , perimeter wall 22, and top wall 23.
  • the perimeter wall 22 is operationally coupled to the bottom wall 2 1 and extends upwardly from the bottom wall 21 .
  • the top wall 23 is operationally coupled to the perimeter wall 22.
  • the bottom wall 21 , perimeter wall 22, and top wall 23 define an interior space 27 which is environmentally separable from an exterior space outside of the reactor vessel 1 1 .
  • the bottom wall 21 and the perimeter wall 22 may be made out of any suitable material such as stainless steel, fiberglass, or concrete. Additionally, the bottom and perimeter walls 22 may have an interior surface lining 24 of epoxy, a polymeric material, or fiberglass . Preferably, the bottom wall 21 and the perimeter wall 22 are constructed out of the same material for ease of production. However at least one embodiment of the present invention contemplates the bottom wall 21 and the perimeter wall 22 being made out of different materials.
  • the top wall 23 may also made out of any suitable material such as stainless steel, fiberglass, or concrete; and may have an interior surface lines with epoxy, a polymeric material, or fiberglass. However, it should be noted that the top wall 23 may be made out of a different material that the bottom wall 21 or the perimeter wall 22. The top wall 23 may be configured as a floating roof.
  • At least one embodiment of the reactor vessel 1 1 is formed substantially in the shape of a sphere, which has a bottom portion, a perimeter portion, and a top portion each corresponding to a bottom wall, perimeter wall and top wall respectively.
  • the bottom wall 21 has a slope from a back side downwardly to a front side.
  • the slope is between 0.075 and 1 .5 inches per linear foot.
  • the bottom wall 21 has a slope from a perimeter downwardly towards a central portion.
  • the slope is between 0.75 and 1 .5 inches per linear foot.
  • the present invention contemplates at least one embodiment, in which at least a portion of the reactor vessel 1 1 abuts an earthen wall 2, such as when at least a portion of the reactor vessel 1 1 is buried.
  • the reactor vessel 1 1 may also include an insulating layer 25 which abuts the earthen wall 2 and provides a thermal insulation between the reactor vessel 1 1 and the earthen wall 2.
  • the reactor vessel 1 1 may also include an access port 26 for facilitating the clean-out and/or repair of the reactor vessel 1 1 .
  • the access port 26 may be located in the top wall 23 , but more preferably is located in the bottom wall 21 or perimeter wall 22.
  • the reactor vessel 1 1 also includes a thermal conditioning unit 34, which has a thermal transfer portion 35operationally coupled to the perimeter wall 22.
  • the thermal transfer portion may include either a fluid jacket or an electrical heating coil, which encompasses at least a portion of the perimeter wall 22.
  • the reactor vessel 1 1 also includes a culture conditioning chamber 37.
  • the culture conditioning chamber 37 is environmentally coupleable with the interior space 27 and is operationally coupled to the thermal transfer portion 35.
  • the culture conditioning chamber 37 may be used for thermally preconditioning a quantity of culture and media prior to introducing the culture and media into the interior space 27 of the reactor vessel 1 1 .
  • the reactor vessel 1 1 may also include at least one sparger 40, positioned substantially within the interior space 27.
  • the sparger 40 is operationally coupled to an input gas stream.
  • a single sparger 40 either a mixed gas must be used as the input gas stream or a mixing assembly may be used to mix various gases from various prior to being introduced into the interior space 27.
  • an array of spargers 41 is used. Each one of the array of spargers 41 is operationally coupled to an associated input gas stream.
  • the array of spargers 41 may include at least one of each of the following: a Carbon Dioxide (CO2) sparger 42 , a
  • Hydrogen (H2) sparger 43 Hydrogen (H2) sparger 43, a Hydrogen Sulfide (H2S) sparger 44, a Carbon Monoxide (CO) sparger 45 , and/or a Nitrogen (N) Sparger 46.
  • H2S Hydrogen Sulfide
  • CO Carbon Monoxide
  • N Nitrogen
  • At least one H2 sparger 43 is positioned vertically above at least one CO2 sparger 42, and at least one H2S sparger 44 is positioned vertically above at least one H2 sparger 43 and at least one CO sparger 45 is positioned vertically above at least one H2 S sparger 44.
  • the Nitrogen sparger 45 can be particularly useful when the reactor is used at least partially for the creation of biomass.
  • the biomass created in the reactor vessel 1 1 during normal operation may range of approximately 12 grams per liter of effective reactor volume per hour.
  • any one of the spargers may be a ring-type sparger, a bayonet type sparger, or any other appropriate configuration.
  • the spargers create bubbles approximately 1 to 10 microns in diameter.
  • the reactor vessel 1 1 also includes an oxidation reduction potential (ORP) control system 50.
  • ORP oxidation reduction potential
  • the oxidation reduction potential control system 50 further includes an oxidation reduction potential probe 5 1 , oxidation reduction potential measurement unit 52, and an oxidation reduction potential adjustment unit 53.
  • the oxidation reduction potential probe 51 is positioned at least partially within the interior space 27 or a culture/media recycling tube .
  • the oxidation reduction potential probe 51 measures an oxidation reduction potential of a culture/media solution positioned in the interior portion.
  • the oxidation reduction potential measurement unit 52 is operationally coupled to the oxidation reduction potential probe 51 and compares an output of the oxidation reduction potential probe 51 to a predetermined ORP upper value and/or a predetermined ORP lower value.
  • the oxidation reduction potential adj ustment unit 53 injects a first oxidation reduction buffer agent 54 into the interior space 27 when the oxidation reduction potential measurinism unit 52 determines the output of the oxidation reduction potential probe 5 1 is at least trending towards the predetermined ORP upper value.
  • the oxidation reduction potential adjustment unit 53 injects a second oxidation reduction buffer agent 55 into the interior space 27 when the oxidation reduction potential measuridging unit 52 determines the output of the oxidation reduction potential probe 51 is at least trending towards the predetermined ORP lower value.
  • the first oxidation reduction buffer agent 54 is either H2S or H2.
  • the ORP upper value is between -400 and -600 mV and more preferably, is approximately -500 mV.
  • the second oxidation reduction buffer agent 55 is CO.
  • the ORP lower value is between -600 and - 800 mV and more preferably is approximately -700 mV.
  • the reactor vessel 1 1 also includes a pH control system 60.
  • the pH control system 60 further includes a pH probe 61 , a pH measurement unit 62, and a pH adjustment unit 63.
  • the pH probe 61 is positioned at least partially within the interior space 27 or a culture/media recycling tube 73, and measures a pH of a culture/media solution positioned in the interior portion.
  • the pH measurement unit 62 is operationally coupled to the pH probe 61 and compares an output of the pH probe 61 to a predetermined pH upper value and/or a predetermined pH lower value.
  • the pH adjustment unit 63 injects a pH buffer agent 64 into the interior space 27 when the pH measurement unit 62 determines the output of the pH probe 61 is at least trending towards the predetermined pH upper value.
  • the pH adjustment unit 63 injects a second pH buffer agent 65 into the interior space 27 when the pH measurement unit 62 determines the output of the pH probe 61 is at least trending towards the predetermined pH lower value.
  • the first pH buffer agent 64 includes CO2, and the pH upper value is between 7.5 and 9, and more preferably the pH upper value is approximately 8.
  • the second pH buffer agent 65 is selected from a group of agents including sodium hydroxide, potassium hydroxide, calcium hydroxide, sodium bicarbonate, ammonia, ammonium and ammonium nitrate.
  • the pH lower value is between 6 and 8, and more preferably is approximately 7.6.
  • the second buffer agent 65 is selected at least in part based upon the rate of change of the pH of the culture/media in the interior space 27 of the reactor vessel 1 1 .
  • the reactor vessel 1 1 also includes an agitation system 76.
  • the agitation system 76 further includes an agitation drive means and an impeller 77.
  • the impeller 77 operationally coupled to the agitation drive means, the impeller 77 positioned within the reactor vessel 1 1 .
  • a motor electrically coupled to a variable frequency drive to control the speed of the motor may be magnetically coupled to an agitation shaft positioned within the reactor.
  • the impeller 77 is thus operationally coupled to the motor.
  • the impeller 77 rotates at between 1 1 00 and 2 1 00 rpm.
  • the impeller 77 rotates at between 1 500 and 1 800 rpm.
  • the impeller 77 rotates at greater than 1 1 0% of the resonance of the reactor vessel 1 1 .
  • Resonance being defined as the sympathetic frequency of vibration for the reactor vessel 1 1 .
  • the impeller 77 may be any physical configuration appropriate for the form factor of the interior space 27 of the reactor vessel 1 1 .
  • the impeller 77 is a rushton impeller.
  • the magneti c coupling unit 78 may be operationally coupled to the top wall 23 or the perimeter wall 22.
  • the interior space 27 further includes a culture/media holding space 28 and a head space 29.
  • a volume of the culture/media holding space 28 to a volume of the head space 29 has a ratio between 1 .5 : 1 to 5 : 1 .
  • a volume of the culture/media holding space 28 to a volume of the head space 29 has a ratio of approximately 2.57: 1 .
  • the reactor vessel 1 1 has an overall interior height between 1 0 and 220 feet.
  • the reactor vessel 1 1 has an overall interior height between 60 and 1 50 feet.
  • the reactor vessel 1 1 has an overall interior height of approximately 140 feet.
  • the reactor vessel 1 1 has an overall interior volume between 75000 and 300000 gallons.
  • the reactor vessel 1 1 has an overall interior volume of 250000 gallons, with an overall interior height of approximately 140 feet, and a volume of the culture/media holding space 28 to a volume of the head space 29 has a ratio of approximately between 2.3 : 1 and 2.8: 1 .
  • the reactor vessel 1 1 further includes a culture/media recirculating system 70.
  • the culture/media recirculating system 70 further comprising a recirculation output port 71 , a recirculation pump 72, a recirculation tube 73 , and a recirculation input port 74.
  • the recirculation output port 71 is environmentally coupled to the interior space 27.
  • the recirculation pump 72 operationally coupled to the recirculation output port 71 .
  • the recirculation input port 74 is environmentally coupled to the interior space 27 and operationally coupled to the recirculation pump 72.
  • the reactor vessel 1 1 may include a plurality of ports for facilitating routing of materials into and out of the interior space 27 of the reactor vessel 1 1 .
  • This plurality of ports may include an input material stream port 12 , an output material stream port 1 3 , biomass removal port 15 , culture/media input port 1 6, and/or a culture sampling port 17. Some of these ports may be environmentally coupled to the interior space 27 through a recycling tube 73 or other intermediate structure.
  • the reactor vessel 1 1 may also include a secondary vessel 57 environmentally coupled to the output material stream port 1 3.
  • the secondary vessel 57 is a condenser.
  • the condenser has a cooling j acket 58 to facilitate the removal of moisture and/or foam from the output material stream.
  • moisture and/or foam may be returned into the interior space 27 of the reactor vessel 1 1 or disposed of through a drain port 59 in the secondary vessel 57.
  • the secondary vessel 57 may be a non-thermal separation system, such as a reverse osmosis system.
  • the reactor vessel 1 1 further includes a data system 67 operationally coupled to at least one of the culture media recirculation system 70, oxidation reduction potential control system 50, pH control system 60, agitation system 76, thermal conditioning unit 34, or at least one sparger 40.
  • the reactor vessel 1 1 further includes a hydrogen diffuser 48 system positioned substantially within the interior space 27 for releasing hydrogen from a mixed gas stream flowing through the hydrogen diffuser 48 system into the interior space 27.
  • the hydrogen diffuser 48 system is operationally coupled between an input material stream port 12 and a first output material stream port 13.
  • the first output material stream port 13 is operationally coupled to an input of an intermediate processing unit 49providing a filtering function.
  • the intermediate processing unit preferably includes an output operationally coupled to a second input material stream port 12 environmentally coupled to the interior space 27.
  • filtering means such as PSA and water-gas shift.
  • the hydrogen diffuser 48 system is operationally coupled between a first output material stream port 13 and a second output material stream port 14.
  • the hydrogen diffuser 48 system further includes a length of tubing having a perimeter wall 22 permeable by hydrogen and substantially impermeable to other components in the mixed gas stream.
  • the present invention also contemplates the interior space 27 of the reactor vessel 1 1 having a plurality of zones.
  • the plurality of zones includes a tank pressure zone 30 having a greater pressure due to the column of culture/media within and above the tank pressure zone 30.
  • the plurality of zones includes a diffuser zone 3 1 , and the hydrogen diffuser 48 system is positioned substantially within the diffuser zone 3 1 .
  • the plurality of zones includes an agitation and defoaming zone 32.
  • the diffuser zone 3 1 is positioned vertically above the tank pressure zone 30 and the agitation and defoaming zone 32 is positioned vertically above the diffuser zone 3 1 .
  • the interior space 27 is designed for holding a vertical column of media/culture of at least 50 feet.
  • the interior space 27 is designed for holding a vertical column of media/culture of at least 1 00 feet.
  • the reactor vessel 1 1 may include a defoaming bar 79 positioned substantially within the agitation and defoaming zone 32. Additionally, a defoaming agent input port 1 8 may be environmentally coupled with the interior space 27 for the selective introduction of a defoaming agent into the interior space 27.

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Abstract

L'invention porte sur un réacteur méthanogène pour la production de méthane, de biomasse cellulaire et d'autres produits utiles destinés à être utilisés dans la fabrication de produits chimiques de spécialité. Le réacteur méthanogène comprend une paroi de fond, une paroi périmétrique et une paroi supérieure délimitant un espace intérieur pouvant être isolé du milieu externe au réacteur, destiné à contenir une culture méthanogène et un milieu de croissance. Le réacteur comprend également au moins un injecteur de gaz situé en grande partie dans l'espace intérieur, servant à faciliter l'acheminement dans le réacteur d'un courant de gaz d'entrée devant être mis en contact avec la culture méthanogène. Le réacteur comprend également un orifice pour courant de matière de sortie, laissant sortir un courant de matière de sortie créé au moins en partie par la culture méthanogène.
PCT/US2009/001896 2009-03-27 2009-03-27 Réacteur méthanogène Ceased WO2010110773A1 (fr)

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PCT/US2009/001896 WO2010110773A1 (fr) 2009-03-27 2009-03-27 Réacteur méthanogène

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013010764A1 (fr) * 2011-07-16 2013-01-24 Université de Mons Procédé et appareil pour l'analyse de systèmes chimiques et/ou biologiques aquatiques
IT202000006325A1 (it) * 2020-03-25 2021-09-25 Biokw Srl Metodo per la valorizzazione energetica di biomasse ed impianto per realizzare tale metodo
EP4474470A1 (fr) * 2023-06-10 2024-12-11 Université de Lorraine Réacteur et procédé de méthanation biologique ex situ
EP4640814A1 (fr) * 2024-04-23 2025-10-29 Prüf- und Forschungsinstitut Pirmasens e.V. Dispositif et procédé pour augmenter les taux de conversion dans la méthanisation biologique

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