WO2012153189A2 - Procédé et système de production de biogaz à partir de la digestion anaérobie de biomasse végétale en phase solide - Google Patents

Procédé et système de production de biogaz à partir de la digestion anaérobie de biomasse végétale en phase solide Download PDF

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WO2012153189A2
WO2012153189A2 PCT/IB2012/001034 IB2012001034W WO2012153189A2 WO 2012153189 A2 WO2012153189 A2 WO 2012153189A2 IB 2012001034 W IB2012001034 W IB 2012001034W WO 2012153189 A2 WO2012153189 A2 WO 2012153189A2
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reactor
process according
hydrolysis
anaerobic
biomass
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WO2012153189A3 (fr
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Adrianus CORNELIUS VAN HAANDEL
Claudia RODRIGUES BARBOSA
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Cetrel SA
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    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C5/00—Other processes for obtaining cellulose, e.g. cooking cotton linters ; Processes characterised by the choice of cellulose-containing starting materials
    • D21C5/005—Treatment of cellulose-containing material with microorganisms or enzymes
    • 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
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/02—Means for pre-treatment of biological substances by mechanical forces; Stirring; Trituration; Comminuting
    • 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
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/20—Heating; Cooling
    • 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
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C1/00—Pretreatment of the finely-divided materials before digesting
    • D21C1/02—Pretreatment of the finely-divided materials before digesting with water or steam
    • 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
    • C12P2203/00—Fermentation products obtained from optionally pretreated or hydrolyzed cellulosic or lignocellulosic material as the carbon source
    • 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 is part of the field of green technology by producing biogas from plant biomass in reactors operated in a semicontinuous or continuous process.
  • sugarcane is a potential energy generator, with the advantage of being completely renewable. Brazil is in a very favorable situation regarding sugarcane production, and until the second half of November 2008, approximately 460 million tons of sugarcane were processed in the 2008/2009 harvest. In 2010, approximately 654 million tons of sugarcane were processed in the 2009/2010 harvest.
  • sugarcane straw and bagasse As a consequence of the increase in ethanol production in recent years, there is the increase of agro-industrial residues from this process, such as sugarcane straw and bagasse.
  • the sugarcane waste production potential (dry matter) represents on average 14% of the sugarcane mass.
  • duos straw and sugarcane bagasse
  • the accumulation is approximately 183 million tons of waste (straw and sugarcane bagasse).
  • the composition of sugarcane bagasse and straw is variable; The largest component is cellulose (40-50%), followed by hemicellulose (20-30%) and lignin (25-35%). Ashes, phenolic compounds, fatty acids and other constituents, called extractives, make up the remaining fraction of these plant biomasses (Reddy, N.; Yang, Y. Biofibers from agricultural byproducts for industrial applications. Trends in Biotechnology, v.23, p 22-27, 2005).
  • the cellulosic and hemicellulosic fractions may be hydrolyzed and converted to fermentable sugars by physical (eg steam blast), chemical (eg alkali, acid, solvent, gas) and biological (eg enzyme or fungal) methods.
  • sugarcane bagasse and residual straw As economic alternatives for the use of sugarcane bagasse and residual straw, the following can be cited as examples: use as fuel in industrial / farm boilers, use in the paper and cardboard industry, use in microbial biomass production and use in feed. animals.
  • sugarcane residue volume can also be verified in other crops such as rice (rice husk), corn (maize straw), barley (barley straw), wheat. (wheat straw), wood (eucalyptus chips) and banana (banana pseudostem). All of this plant biomass has been the subject of a series of studies for applications in green technologies to obtain products of industrial interest, such as alcohols (eg ethanol, butanol), organic acids (eg lactic, acetic, citric acid). ) and biogas.
  • alcohols eg ethanol, butanol
  • organic acids eg lactic, acetic, citric acid
  • Anaerobic digestion is a process performed by a consortium of microorganisms under anaerobic conditions (absence of oxygen) converting complex organic material into simpler compounds and cellular material.
  • the biogas generated is composed of methane, carbon dioxide, water, hydrogen sulfide gas, ammonia, among others, depending on the biomass composition employed.
  • the process is developed in sequential stages involving complex metabolic processes, which depend on the activity of at least four groups of microorganisms, namely: hydrolytic bacteria, responsible for the release of exoenzymes that catalyze the hydrolysis of complex organic polymers such as pectin, hemicellulose and cellulose to sugars, long chain carboxylic acids and glycerol; acidogenic bacteria, which metabolize hydrolysed products to even simpler ones such as short chain carboxylic acids, alcohols, lactic acid, CO 2 , H 2 , NH 3 and H 2 S as a function of environmental conditions; acetogenic bacteria that convert the products resulting from acidogenic metabolism into acetate, hydrogen and carbon dioxide and, finally, these are converted to methane and carbon dioxide by methanogenic bacteria (Chernicharo, CAL. Anaerobic Reactors. Department of Engineering Sanitary and Environmental-UFMG, 246p., 1997).
  • hydrolytic bacteria responsible for the release of exoenzymes that catalyze the hydrolysis of complex organic poly
  • the temperature in the anaerobic digestion process has a strong influence on the conversion rate of organic material and on the predominant species in a certain temperature range.
  • Alkalinity of a system is its ability to neutralize acids as a result of the presence of chemical species of alkaline nature. Alkalinity is indicative of the buffering capacity of a given system and therefore for high alkalinity it should not be It should be understood that the pH is necessarily high. Volatile fatty acids are closely related to alkalinity. The acids formed in the process tend to lower the pH making it acidic and unsuitable for anaerobic processes. In this sense the buffering effect of the solution avoids sudden drops and frequent pH fluctuations (Chernicharo, CAL. Anaerobic Reactors. Department of Sanitary and Environmental Engineering-UFMG, 246p., 1997).
  • the present invention differs from the above by the type of pretreatment employed (steam blast) and the possibility of addition of catalyst (industrial enzymes) combined with anaerobic bacteria to increase productivity and digestion efficiency. Additionally, anaerobic sludge is selected from industrial and domestic effluent treatment plants, and the industrial or domestic effluent digestion step is not part of this invention.
  • Cellulases are usually a mixture of several enzymes that catalyze cellulose hydrolysis, converting it into reducing sugars (mainly glucose) that can be used by microorganisms to produce industrially interesting inputs.
  • reducing sugars mainly glucose
  • the present invention relates to a process for producing biogas from lignocellulosic materials, comprising the steps of:
  • step (a) by anaerobic bacteria, with or without the addition of cellulase enzymes, together or not with xylanase enzymes, where steps (a) and (b) are performed in separate reactors, step (b) is performed in a The only reactor and the products from step (b) are biogas and digested biomass.
  • the present invention further relates to a system for carrying out the biogas production process also object of the invention which comprises:
  • step (ii) a second reactor for hydrolysis and anaerobic digestion of the material treated in step (i) by anaerobic bacteria with or without the addition of cellulase enzymes together or not with xylanase enzymes.
  • the hydrolysis step may be initiated prior to step (b) in an intermediate reactor with the addition of anaerobic bacteria and enzymes operated under thermophilic condition.
  • Figure 1 - Figure 1 is a schematic representation of the system and process of biogas production from plant biomass, with a steam blast pretreatment reactor (10) and an anaerobic digestion reactor (20) without addition of catalyst (mesophilic or thermophilic temperature).
  • Figure 2 - Figure 2 corresponds to the schematic representation. of the system and process of biogas production from plant biomass, with a steam blast pretreatment reactor (10) and an anaerobic digestion reactor (20), with catalyst addition (mesophilic or thermophilic temperature ).
  • FIG 3 - Figure 3 is a schematic representation of the system and process of biogas production from plant biomass, with a steam blast pretreatment reactor (10), an intermediate reactor (15) to initiate hydrolysis. in thermophilic condition with addition of catalyst and anaerobic bacteria and an anaerobic digestion reactor (20) (thermophilic temperature).
  • the present invention relates to a process of producing biogas from lignocellulosic materials, which comprises the steps of:
  • step (b) hydrolysis and anaerobic digestion of material treated in step (a) by anaerobic bacteria, with or without the addition of cellulase enzymes together or not with xylanase enzymes, wherein steps (a) and (b) are carried out.
  • step (b) is performed in a single reactor and the products of step (b) are biogas and digested biomass.
  • hydrolysis may be previously initiated in an intermediate reactor between steps (a) and (b) under thermophilic condition.
  • the production of biogas according to the invention is made from vegetable biomass, which can be selected from the group consisting of: sugarcane bagasse, sugarcane straw, rice husk, corn, barley straw, wheat straw, eucalyptus chips, banana pseudostem and mixtures thereof.
  • the first process step of the invention comprises pretreatment of the lignocellulosic material into a first reactor (10) by steam explosion as shown schematically.
  • a first reactor 10
  • Hemicellulose due to its amorphous structure and lower degree of polymerization than cellulose, is partially or completely hydrolyzed in this pretreatment step, depending on the reaction conditions employed.
  • Said pretreatment also aims at destroying the plant biomass fiber, reducing crystallinity and increasing porosity, in order to facilitate hydrolysis of the cellulosic fraction.
  • the pretreatment of process step (a) of the invention comprises steam explosion by the application of water vapor to the plant biomass in said first reactor, with temperatures ranging from 150-300 ° C, preferably 160-260 °. C, which corresponds to pressures of 0.62-4.7MPa and reaction time ranging from a few seconds to a few minutes before decompression. Even more preferably, the reaction should be carried out at temperatures in the range of 180-220 ° C and reaction times of 3-15 minutes.
  • the steam explosion process is the sudden decompression of a pressurized system containing high pressure saturated water vapor and plant biomass. Water under high pressure penetrates the cell structure of the biomass, hydrates the cellulose and hydrolyzes the hemicellulose.
  • CHEN and others Simultaneous saccharification and fermentation of steam exploded wheat straw pretreated with alkaline peroxide. Process Biochemistry. V. 5-9, 2008).
  • the pentoses of the hemicellulosic fraction can be separated and access of enzymes to cellulose is facilitated.
  • sugars from the hemicellulosic fraction may be transferred to the liquid phase by a biomass wash step, and this liquid rich in organic material may be sent directly to the anaerobic digester.
  • Pretreated biomass has humidity around 55-60%.
  • the second process step of the invention comprises hydrolysis and anaerobic digestion of the material treated in step (a) in a second reactor (20).
  • the material treated in step (a) undergoes hydrolysis and anaerobic digestion in said reactor (as shown in figures 1, 2 and 3), which can operate under mesophilic or thermophilic conditions, with a temperature in the range of 20-70 ° C. preferably from 37 to 55 ° C.
  • Anaerobic bacteria Robots are added to the reactor, which should be operated at a pH of 5.0-8.0, preferably 6.0-8.0, even more preferably 6.5-7.5.
  • the total solids concentration in the anaerobic digestion and hydrolysis reactor is in the range of 5-50%, preferably 5-15%.
  • the feed of said reactor may be semicontinuous or continuous.
  • Industrial enzymes can be added to anaerobic digestion combined with anaerobic bacteria to increase the efficiency of hydrolysis and anaerobic digestion.
  • the pH in step (b) may be controlled by the addition of alkalizing agents (strong or weak bases), preferably sodium hydroxide or urea.
  • alkalizing agents strong or weak bases
  • pH control can be obtained by recirculating the material contained in the reactor, with or without the addition of alkalinizers.
  • the cellulosic and hemicellulosic fractions can be converted to lower molecular weight compounds by anaerobic bacteria and commercial enzymes, cellulases with or without xylanases, with the aim of increasing the efficiency and productivity of the reactions. hydrolysis and anaerobic digestion.
  • the fungus Trichoderma reesei is the most industrially used microorganism for the production of cellulases and xylanases, but some bacteria are also capable of producing such enzymes, such as Clostridium thermocellum, Ruminococcus albus and Streptomyces sp. (Corridor and others Pretreatment and Enzymatic Hydrolysis of Sorghum Bran. Cereal Chemistry, v.84, p.61-66, 2007).
  • Anaerobic bacteria can be selected from anaerobic sludges from wastewater treatment plants or solid domestic or industrial waste.
  • the microorganisms must be adapted to the medium containing the biomass employed for a period ranging from 20-90 days.
  • the most suitable volumetric organic load applied to the reactor is in the range of 5-25 g COD / L.day, more preferably 10-20 g COD / L.day. This organic load should be increased slowly, ensuring conditions that favor the development of anaerobic bacteria.
  • the type and dosage of enzymes employed in the process of hydrolysis and anaerobic digestion are dependent on factors such as biomass composition, degree of crystallinity of the polymeric chain, type of pretreatment employed and process conditions, especially temperature and pH.
  • Hydrolysis of the cellulosic fraction of plant biomass for biogas production may be carried out by the addition of cellulases in amounts of about 0.05-5% by mass of total solids (ST), more preferably 0.5-2.5. Mass% ST.
  • the xylanase is added in an amount sufficient to hydrolyze hemicellulose to xylose at concentrations of 0.001-1 wt.% ST, more preferably 0.05-0.2 wt.%.
  • treatment of hemicellulose with the addition of xylanase is not mandatory according to the present invention after steam blast pretreatment.
  • the anaerobic bacteria of said second reactor (step (b)) are obtained by inoculating the same with 5-40% v / v anaerobic sludge, preferably 10-20% v / v.
  • Such inoculation aims at the conversion of carbohydrates produced in the hydrolysis reaction to organic acids, which can be converted to methane and carbon dioxide in this same reactor of step (b).
  • said second reactor may further comprise a solution of organic nutrients, to provide a suitable medium for the development of anaerobic bacteria.
  • the ideal nutrient solution should contain macro (N-NH 4 + , P-P0 4 3 " , Mg, Ca) and micronutrients (Fe, Ni, Zn, Co, etc.) as well as alkalinity (NaHC0 3 or KH 2 P0 4 and K 2 HP0 4 ) (Aquino et al. Journal of Sanitary and Environmental Engineering, v.12, n. 2, p. 192-201, 2007)
  • a fraction of the nutrient solution can be composed of vinasse (5-10). 20%), by-product of the distillation process for ethanol production from sugar and alcohol plants.
  • step (b) the microorganisms present in the sludge perform all the stages of conversion of organic matter to biogas (hydrolysis, acycogenesis, acetogenesis and methanogenesis) in the same reactor.
  • a solid / liquid separation step is not required prior to step (b) as the Anaerobic digestion occurs in the semi-solid phase.
  • the digested bagasse may be subjected to solid / liquid separation with recirculation of one of the phases to the solid phase digestion reactor. At this stage filtration, centrifugation or pressing can be used, and the fraction to be recirculated (solid or liquid) to the reactor will be dependent on the separation method employed.
  • the parameters monitored in the aaerobic digestion and hydrolysis reactor (step (b)) to assist in monitoring reactor stability and performance are pH, temperature, alkalinity, volatile fatty acids, COD (Chemical Oxygen Demand), total solids, suspended solids, volatile solids, biomass density and humidity.
  • the present invention further relates to a system for carrying out the biogas production process also object of the invention which comprises:
  • step (ii) a second reactor for hydrolysis and anaerobic digestion of material treated in step (i) by anaerobic bacteria.
  • hydrolysis and anaerobic digestion steps may be performed in separate reactors.
  • the hydrolysis step can be started in an intermediate reactor (15), as shown in Figure 3, between steps (a) and (b) in the thermophilic condition with anaerobic bacteria, with addition of cellulase enzymes, with or without the addition of xylanases.
  • Sugarcane bagasse was used as biomass material, which was pre-treated in a first steam blast reactor (10), using temperatures of 200 ° C, pressure of 1, 6 MPa (16 bar) and reaction time of 7 minutes. The humidity of the expelled bagasse was around 50%.
  • the pretreated bagasse was transferred to the second anaerobic digestion reactor (20). Said reactor was inoculated with 20% v / v sludge anaerobic treatment of a brewery effluent treatment system adapted to the substrate (pretreated bagasse).
  • the total volatile solids concentration of the obtained sludge was 32gSTV.L "1 and specific methanogenic activity (AME) of 0.3gDQO.gSTV ⁇ .day " 1 using standard substrate.
  • AME specific methanogenic activity
  • the process was carried out under thermophilic condition, temperature around 50 ° C, pH around 7.0, solids concentration around 10%, with retention time of 20 days and semicontinuous feeding.
  • the digested bagasse was submitted to solid / liquid separation and the solid fraction recirculated to the digester.
  • the parameters monitored in the second reactor to assist in monitoring its stability and process performance were: pH, temperature, alkalinity, volatile fatty acids, COD, total solids, suspended volatile solids, total volatile solids, total fixed solids, bagasse density and moisture and cake density and moisture.
  • FIG 1 shows schematically the system and process presented in this example.
  • Sugarcane bagasse was used as biomass material, which was pre-treated in a first steam explosion reactor (10), using temperatures of 200 ° C, 1.6 MPa (16 bar) and reaction time of 7 minutes. The humidity of the exploded bagasse was around 50%.
  • the pretreated bagasse was transferred to the second anaerobic digestion reactor (20).
  • Said reactor was inoculated with 20% v / v anaerobic sludge, with total volatile solids concentration of 32gSTV.L "1 and specific methanogenic activity (AME) of 0.3gDQO.gSTV ⁇ 1 .day " 1 using standard substrate, and with a commercial enzyme cocktail composed of cellulases and xylanases.
  • the sludge was purchased from an anaerobic digestion unit of brewery effluents and adapted to the substrate used (pretreated bagasse).
  • the process was carried out under thermophilic condition, with temperature around 50 ° C, pH around 7.0, solids concentration around 10%, retention time of 20 days and semicontinuous feeding.
  • the digested bagasse was submitted to solid / liquid separation and the solid fraction recirculated to the digester.
  • the parameters monitored in the second reactor to assist in monitoring its stability and performance were: pH, temperature, alkalinity, volatile fatty acids, COD, total solids, suspended volatile solids, total volatile solids, total fixed solids, density and bagasse moisture and cake density and moisture.
  • FIG. 2 shows schematically the process and system presented in this example.
  • Sugarcane bagasse was used as biomass material, which was pre-treated in a first steam explosion reactor (10), using temperatures of 200 ° C, 1.6 MPa (16 bar) and reaction time of 7 minutes. The humidity of the exploded bagasse was around 50%.
  • the exploded bagasse was transferred to a hydrolysis reactor (15) and inoculated with 20% v / v anaerobic sludge, with total volatile solids concentration of 32gSTV.L "1 and specific methanogenic activity (AME) of 0.3gDQO.gSTV "1 day '1 using standard substrate, and with a commercial enzyme cocktail composed of cellulases and xylanases.
  • the sludge was purchased from an anaerobic digestion unit of brewery effluents and adapted to the substrate used (pretreated bagasse).
  • the bagasse cellulosic and hemicellulosic fractions are converted to lower molecular weight compounds (sugars, alcohols and organic acids) by sludge enzymes and bacteria.
  • the process was carried out under thermophilic condition, with temperature around 50 ° C, pH around 5.0, solids concentration around 10%, and retention time of 2 days.
  • the pre-treated bagasse was fed in batches.
  • the solid and liquid fractions from the hydrolysis reactor were transferred to the anaerobic digestion reactor (20) with semicontinuous feeding.
  • Said reactor was inoculated with 30% v / v anaerobic sludge with total volatile solids concentration of 32gSTV.L "1 and specific metagenogenic activity (AME) of 0.3gDQO.gSTV ⁇ 1 .day " 1 using standard substrate. .
  • the sludge was purchased from an anaerobic digestion unit of brewery effluents and adapted to the substrate used (pretreated bagasse).
  • the reactor was operated in thermophilic condition, with temperature around 50 ° C, pH around 7.0, solids concentration around 10%, and retention time of 20 days. After the digestion step, the digested bagasse was submitted to solid / liquid separation and the solid fraction recirculated to the digester.
  • FIG. 3 shows schematically the process and system presented in this example.

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Abstract

La présente invention concerne un procédé de production de biogaz à partir de matières lignocellulosiques, comprenant les étapes suivantes: (a) traitement de biomasse végétale par explosion à la vapeur; et (b) hydrolyse et digestion anaérobie de la matière traitée dans l'étape (a) par des bactéries anaérobies; les étapes (a) et (b) étant réalisées dans des réacteurs séparés, l'étape (b) étant réalisée dans un unique réacteur et les produits de l'étape (b) étant le biogaz et la biomasse digérée. En variante, l'hydrolyse et la digestion peuvent être réalisées dans des réacteurs séparés. La présente invention concerne également un système pour la réalisation du procédé de production de biogaz également objet de l'invention, comprenant: (i) un premier réacteur pour le traitement de biomasse végétale par explosion à la vapeur; et (ii) un second réacteur pour l'hydrolyse et la digestion anaérobie de la matière traitée dans l'étape (i) par des bactéries anaérobies. Dans un mode de réalisation préféré, les procédés et systèmes de l'invention peuvent en outre faire intervenir, dans le réacteur d'hydrolyse et de digestion anaérobie, des enzymes cellulases avec ou sans addition de xylanases. Dans une autre configuration, l'hydrolyse peut se produire dans des réacteurs séparés.
PCT/IB2012/001034 2011-05-11 2012-05-25 Procédé et système de production de biogaz à partir de la digestion anaérobie de biomasse végétale en phase solide Ceased WO2012153189A2 (fr)

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WO2018226170A3 (fr) * 2017-06-07 2019-03-07 Ptt Global Chemical Public Company Limited Souche mutante de clostridium thermocellum pour la production de cellulase et de xylanase et procédé de préparation associé
US10233592B2 (en) * 2014-10-03 2019-03-19 Nafici Environmental Research Method for processing straw
WO2019099953A1 (fr) * 2017-11-16 2019-05-23 Hansen Jaron C Prétraitement microbien pour la conversion de biomasse en biogaz
WO2023086493A1 (fr) * 2021-11-10 2023-05-19 The Penn State Research Foundation Procédé pour la production de biogaz de haute pureté à partir d'une matière première lignocellulosique

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