EP3172331A1 - Procédé de production de molécules organiques à partir de biomasse fermentescible - Google Patents
Procédé de production de molécules organiques à partir de biomasse fermentescibleInfo
- Publication number
- EP3172331A1 EP3172331A1 EP15756198.6A EP15756198A EP3172331A1 EP 3172331 A1 EP3172331 A1 EP 3172331A1 EP 15756198 A EP15756198 A EP 15756198A EP 3172331 A1 EP3172331 A1 EP 3172331A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- fermentation
- fatty acids
- volatile fatty
- microorganisms
- organic molecules
- 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.)
- Pending
Links
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- 239000004324 sodium propionate Substances 0.000 description 1
- 235000010334 sodium propionate Nutrition 0.000 description 1
- 229960003212 sodium propionate Drugs 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
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- 235000000346 sugar Nutrition 0.000 description 1
- 150000008163 sugars Chemical class 0.000 description 1
- 150000003511 tertiary amides Chemical class 0.000 description 1
- UAXOELSVPTZZQG-UHFFFAOYSA-N tiglic acid Natural products CC(C)=C(C)C(O)=O UAXOELSVPTZZQG-UHFFFAOYSA-N 0.000 description 1
- 235000013619 trace mineral Nutrition 0.000 description 1
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- 238000002604 ultrasonography Methods 0.000 description 1
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- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
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- C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
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- C05F1/00—Fertilisers made from animal corpses, or parts thereof
- C05F1/005—Fertilisers made from animal corpses, or parts thereof from meat-wastes or from other wastes of animal origin, e.g. skins, hair, hoofs, feathers, blood
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- C05F1/00—Fertilisers made from animal corpses, or parts thereof
- C05F1/007—Fertilisers made from animal corpses, or parts thereof from derived products of animal origin or their wastes, e.g. leather, dairy products
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- C05F1/00—Fertilisers made from animal corpses, or parts thereof
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- C05F9/00—Fertilisers from household or town refuse
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- C05F9/00—Fertilisers from household or town refuse
- C05F9/02—Apparatus for the manufacture
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- C12M1/00—Apparatus for enzymology or microbiology
- C12M1/107—Apparatus for enzymology or microbiology with means for collecting fermentation gases, e.g. methane
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- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/20—Degassing; Venting; Bubble traps
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- C12M43/00—Combinations of bioreactors or fermenters with other apparatus
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- C12M99/00—Subject matter not otherwise provided for in other groups of this subclass
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- C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
- C12P5/02—Preparation of hydrocarbons or halogenated hydrocarbons acyclic
- C12P5/023—Methane
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- C12P7/00—Preparation of oxygen-containing organic compounds
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- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
- C12P7/52—Propionic acid; Butyric acids
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- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
- C12P7/54—Acetic acid
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B3/00—Electrolytic production of organic compounds
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- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
- Y02A40/10—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in agriculture
- Y02A40/20—Fertilizers of biological origin, e.g. guano or fertilizers made from animal corpses
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- 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
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
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- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/40—Bio-organic fraction processing; Production of fertilisers from the organic fraction of waste or refuse
Definitions
- the present invention relates to a method for producing molecules from fermentable biomass. This production is made from biomass to the production of molecules of interest and directly usable, similar to a production of molecules in a biorefinery.
- the process comprises, inter alia, an anaerobic fermentation step.
- fermentable biomass is meant here an organic substrate, preferably but not exclusively, non-food, obtained from waste, by-products and co-products formed from organic materials, that is to say biomass, resulting from human activities whether domestic, industrial, agricultural, forestry, aquaculture, agro-industrial or livestock.
- organic substrate of manure, the organic fraction of household refuse, slaughterhouse co-products, cellulosic or lignocellulosic residues from agro-industry such as those resulting from the transformation.
- sugar cane bagasse
- sunflower or soy the organic substrate, preferably but not exclusively, non-food, obtained from waste, by-products and co-products formed from organic materials, that is to say biomass, resulting from human activities whether domestic, industrial, agricultural, forestry, aquaculture, agro-industrial or livestock.
- organic substrate of manure, the organic fraction of household refuse, slaughterhouse co-products, cellulosic or lignocellulosic residues from agro-industry such as those resulting from
- anaerobic fermentation is meant a fermentation carried out under anaerobic conditions by microorganisms, eukaryotic or prokaryotic, such as bacteria, fungi, algae or yeasts.
- molecule means here, but not exclusively, so-called precursor molecules. These precursors subsequently allow the production of other molecules which have an energy and / or chemical interest higher than that of the precursors, it being understood that they are organic molecules. Examples of molecules having an energy and / or chemical interest are molecules having a carbon chain, such as acids, hydrocarbons, methane, esters, alcohols, amides or polymers.
- microorganisms used in such processes are generally genetically modified microorganisms.
- precursor molecules are subsequently transformed, by known chemical routes, into different usable molecules. The transformation into final molecules takes place later and independently of the production phase of these so-called precursor molecules.
- US-A-6,043,392 discloses such a process for producing ketones by heat treatment of volatile fatty acid salts obtained by anaerobic fermentation. Part of the volatile fatty acids are also converted into hydrocarbons, aldehydes, alcohols. In addition to a limited number of end products obtained by such a process, it turns out that it is carried out in two distinct stages, namely the fermentation and then the treatment of the AGV salts. In other words, the process is not continuous. It is known that the production of volatile fatty acids carried out by anaerobic fermentation induces an acidification of the medium detrimental to microorganisms.
- AGVs are extracted after a given fermentation time.
- US-A-4,358,537 a process, in situ, for producing carbohydrates from a peat plot.
- AGVs are not a sought-after product as a precursor.
- US-A-2013/309 740 describes an anaerobic fermentation whose object is the production of methane, the AGV is a waste to be eliminated.
- the invention aims more particularly at remedying these drawbacks by proposing a method making it possible to produce, in a regular and controlled manner, various so-called biobased molecules, that is to say molecules derived from biomass, in a biorefinery-type approach.
- the subject of the invention is a process for producing organic molecules from fermentable biomass, comprising an anaerobic fermentation step, said fermentation producing so-called precursor fermentative metabolites, such as volatile fatty acids, these so-called precursor metabolites being transformed into final organic molecules by non-fermentative route, the process comprising at least one step of fermenting an organic substrate formed by fermentable biomass in a fermentation reactor to production as fermentative metabolites of fatty acids volatile compounds (AGV) having a carbon chain of 1 to 8 carbons, characterized in that it comprises at least the following stages: - a) extracting, between the beginning of production and the maximum production of said volatile fatty acids, at least a portion of the volatile fatty acids of the fermentation medium so that the production of fermentative metabolites by the microorganisms is not affected and introduce at least a portion of the liquid phase, containing microorganisms, resulting from the extraction in the fermentation reactor,
- AUV fatty acids volatile compounds
- step a) synthesizing organic molecules from fermentative metabolites produced in the fermentation reactor or volatile fatty acids extracted in step a),
- the extraction step not only makes it possible to avoid the accumulation of volatile fatty acids in the medium, but also to preserve the microorganisms, the extraction being carried out under non-lethal conditions for all the microorganisms.
- the extraction is biocompatible, that is to say that it does not interfere with or degrade the biological medium in which it is carried out.
- the activity of the microorganisms is maintained at a high level, close to the initial level, throughout the fermentation cycle, most of the microorganisms not being inhibited by this extraction step.
- such a method may comprise one or more of the following features:
- step a a mixture of microorganisms from defined natural ecosystems is inoculated in the fermentation reactor.
- Steps a) to c) are carried out continuously.
- the residues from the process are suitable for use as an amendment, fertilizer or as a co-product such as methane.
- the invention also relates to an installation for implementing a method according to one of the preceding characteristics, characterized in that it comprises at least:
- a synthesis organ such as a chemical reactor or an electrolysis cell, capable of ensuring the synthesis of fermentative metabolites obtained during the fermentation into final organic molecules.
- such an installation may include the following features:
- FIG. 1 is a simplified diagram representative of the method that is the subject of the invention.
- the substrate 1 used here is advantageously untreated, namely that it has undergone no physicochemical or enzymatic pretreatment.
- the substrate 1 may have undergone mechanical treatment, for example grinding 2, facilitating the action of microorganisms on the substrate.
- This is mainly constituted by biomass 3 resulting from human activities.
- the substrate 1 has undergone a physicochemical or enzymatic pretreatment, although this mode is not a preferred embodiment.
- the substrate 1 is used as supplied, provided that its fermentable power is preserved.
- This fermentable power is characterized by the methanogenic potential of biomass, commonly referred to as the BMP (Biochemical Methane Potential). Controlled dehydration, as described in patent application FR1302119 filed by the applicant allows to maintain over a period of several months this fermentable power.
- Some substrates also contain organic molecules, such as organic acids, which will not influence, or marginally, the fermentation process.
- organic molecules such as organic acids, which will not influence, or marginally, the fermentation process.
- these molecules can be found in the fermentation medium and participate, for example as a precursor, in the production of the final organic molecules.
- nutrients and / or mineral compounds in order to increase bacterial growth and / or regulate the pH of the substrate and / or co-products promoting the production of AGVs or other molecules.
- nutrients and / or mineral compounds in order to increase bacterial growth and / or regulate the pH of the substrate and / or co-products promoting the production of AGVs or other molecules.
- the addition in a small amount, of NaOH, KOH, Ca (OH) 2 , K 2 HPO 3 , KH 2 PO 3, glycerol or vitamin or trace element solutions. This addition is represented by the arrow A.
- the substrate is introduced into a fermentation reactor 4, known per se and dimensioned for the desired production, whether the latter is on a laboratory scale to carry out tests or on an industrial scale in the case of a production.
- the fermentation reactor 4 or bioreactor has a volume ranging from a few liters to several hundred cubic meters, as needed.
- Microorganisms are advantageously but not mandatory, previously introduced into the fermentation reactor 4, at least during startup, in an amount sufficient to initiate the fermentation. It is conceivable that the quantity of microorganisms introduced depends, among others, on the substrate. These microorganisms are inoculated in the form of a consortium, illustrated by the arrow M. By the term consortium, is meant a mixture or mixture of microorganisms, eukaryotic or prokaryotic, whether bacteria, yeasts, fungi or algae. These microorganisms M come mainly from natural ecosystems suitable for carrying out a fermentation under anaerobic conditions.
- ecosystems the anaerobic zone of aquatic environments such as the anoxic zone of certain lakes, soils, marshes, sewage sludge, the rumen of ruminants or the intestine of termites.
- anoxic zone of certain lakes, soils, marshes, sewage sludge, the rumen of ruminants or the intestine of termites can vary significantly. It turns out that this qualitative and quantitative diversity of microorganisms surprisingly provides a robustness and adaptability to the fermentation process to ensure optimal use of substrates, whatever the composition of the latter and this under conditions variable fermentation.
- the substrate 1 is used as it is, that is to say, it is not sterilized or, more generally, it is not cleared of microorganisms that it contains beforehand. its introduction into the bioreactor, it turns out that these microorganisms endemic to the substrate 1 are, de facto, incorporated in the consortium M or at least associated with the latter in the bioreactor 4.
- the fermentation 5 to produce volatile fatty acids has, according to the process of the invention, interesting characteristics such as being carried out in a non-sterile condition.
- the consortium M of microorganisms makes it possible to optimally use the substrate 1, without adding products such as enzymes.
- the fermentation 5 takes place under anaerobic conditions, more specifically when the redox potential is less than -300mV, advantageously between -550mV and -400mV, when the pH is less than 8, preferably between 4 and 7.
- the fermentation 5 is advantageously limited to the production of fermentative metabolites called precursors, therefore volatile fatty acids or AGV.
- the fermentation carried out according to the invention with the consortium M makes it possible, unlike fermentations with defined strains, to degrade not only the sugars (pentoses, hexoses or others) present in the substrate 1 but also the major part of the substrate 1 components such as proteins, nucleic acids, lipids, carboxylic acids.
- the yield of such fermentation is particularly high, waste production being low.
- the fermentation of complex molecules such as proteins is particularly interesting because it allows, inter alia, the production of isobutyric acid, 2-methyl butyric acid and isovaleric acid.
- These branched volatile fatty acids are precursors with high potential for the production of branched molecules such as branched hydrocarbons which have advantages as a fuel.
- the fermentation 5 produces, among the various compounds generated, precursors for a synthesis of bio-fuels and biomolecules of interest for chemistry.
- this fermentation leads, in a first step, to the formation of volatile fatty acids having from one to eight carbons, mainly from two to four carbons such as acetic acid, propionic acid and butyric acid. .
- Volatile fatty acids with a longer chain, thus greater than four carbons such as valeric and caproic, heptanoic or octanoic acids, are also obtained.
- the metabolites produced in quantity during the fermentation are volatile fatty acids, predominantly of two to six carbons.
- carboxylic acids with long carbon chains (C8 to C22) which will be fermented or transformed, during the subsequent chemical conversion steps, into hydrocarbons such as octane and kerosene.
- carboxylic acids can be added, according to the arrow C, in their raw form or by means of substrates containing them as certain vegetable products which contain oils.
- substrates containing them such as certain vegetable products which contain oils.
- the fermentation can be carried out batchwise or batchwise, continuously batchwise or fed-batch or continuously in one or more fermentation reactors arranged in series.
- Fermentation is performed using conventional fermentation techniques to generate anaerobic conditions. For this the use of a carbon dioxide atmosphere is preferred, although other gases such as nitrogen or argon may be considered to achieve anaerobic conditions.
- the temperature in the fermentation reactor (s) 4 is between 20 and 60 ° C, preferably between 35 and 42 ° C.
- the pH is less than 8, preferably between 4 and 7.
- the redox potential is less than -300mV, advantageously between -550mV and -400mV.
- the means for managing and maintaining the temperature and the pH are known per se.
- the fermentation is maintained for a time sufficient to produce volatile fatty acids in the liquid phase, illustrated by reference 6.
- the fermentation time varies, among others, depending on the substrate 1, the microorganisms M present, the initial concentration of AGV and fermentation conditions.
- the fermentation period is between 1 and 7 days, preferably between 2 and 4 days.
- the concentration of AGV 6 obtained in the fermentation medium at the end of this period is variable, but is generally of the order of 10 to 20 g / L, depending on the volatile fatty acids, it being understood that under certain conditions it can to be greater than 35 g / L for example close to 50 g / l.
- the fermentation medium is at an acidic pH, which is generally between 4 and 6. It is conceivable that fermentation produces other compounds, in particular gases 7, such as dioxide. carbon, hydrogen or methane which, advantageously, are recovered and used in known manner, according to reference 8.
- Carbon dioxide is, for example, reintroduced into the fermentation reactor 4 to participate in the maintenance of anaerobic conditions. Alternatively, it is used as a carbon source for the production of photosynthetic biomass. Other metabolites are produced, for example lactic acid, esters, alcohols. These funds can either be reintroduced into the bioreactor 4, to continue the fermentation 5, or be used for other applications, as is or after transformation.
- the next step is extraction 9 of the volatile fatty acids 6 thus formed.
- These by reactions known per se, will produce, in a next step 10, so-called biosourced molecules, according to the defined needs.
- they form a substrate for a so-called secondary fermentation for produce volatile fatty acids with longer carbon chain.
- This fermentation can be conducted in the same reactor, in the continuity of the first fermentation, or, alternatively, in another reactor.
- mention may be made of the secondary fermentation by certain microorganisms such as Megasphaera edelsnii or Clostridium kluyveri, of acetic and butyric acids into caproic and caprylic acids. Such fermentation thus makes it possible to increase the amounts of certain AGV initially present in a limited amount.
- the volatile fatty acids 6 produced in the liquid phase by the anaerobic fermentation and which are, at least in part, extracted are under conditions such that the extraction 9 does not affect, or at least marginal, the production of volatile fatty acids by the microorganisms present in the fermentation medium.
- volatile fatty acids are extracted from the fermentation medium, de facto acidification of the medium is reduced by these acids.
- the extraction method chosen is not lethal for all the microorganisms
- the residual liquid phase 1 1, after extraction 9 also contains a certain amount of microorganisms. alive, so potentially active.
- this liquid phase 1 1 there is a concentration of volatile fatty acids 6 lower than that of the fermentation medium, it is therefore possible to reinject it into the fermentation reactor 4.
- the pH of the medium is raised, but the medium is also resuspended with microorganisms, ensuring the fermentation 5, by extraction 9 of the acidic compounds 6.
- the extraction 9 is advantageously carried out in the liquid phase. It is conducted continuously or sequentially, for example with extraction every 12 hours. In all cases, the extraction of a part of the volatile fatty acids is carried out between the beginning of production and the maximum production of metabolites.
- the extraction is carried out near the threshold of inhibition of microorganisms by volatile fatty acids. This threshold depends on, among other things, the substrate and the fermentation conditions.
- the introduction of the liquid phase resulting from the extraction is carried out within a period which makes it possible to maintain a high level of production of the volatile fatty acids, that is to say close to the level at which the extraction has been made. .
- the volatile fatty acids 6 are purified 12 and / or transformed, according to the step referenced 10, into other products, such as alkanes, alkenes, amides, amines, esters, polymers and the like. by techniques known per se such as distillation, electrosynthesis, esterification, amidation or polymerization.
- a part of the volatile fatty acids 6 produced during the fermentation is not extracted but undergoes an electrosynthesis or electrolytic synthesis step.
- hydrocarbons are produced, primarily from volatile fatty acids long carbon chain to acetate.
- Electrosynthesis step 13 converts volatile fatty acids produced in large amounts of gaseous and liquid compounds via the known reactions of Kolbe and / or Hofer-Moest electrochemical decarboxylation. These two reactions occur simultaneously during the electrolysis synthesis but an adjustment is possible to favor one or the other of these reactions by modifying easily controllable parameters as described below. Various metabolites can be produced by playing on these parameters, which allows a flexible production of different molecules, both qualitatively and quantitatively.
- Electrosynthesis 13 makes it possible to convert the volatile fatty acids directly into the fermentation medium. As a result, electrosynthesis is also a means of extracting volatile fatty acids from the fermentation medium. When other organic molecules such as carboxylic acids or alcohols are added to the volatile fatty acids, the range of hydrocarbons and products that can be formed increases.
- the Applicant has found that the electrosynthesis step can be carried out in the fermentation medium, under mild reaction conditions, at ambient temperature and pressure, at 3V or more than 3V and at 1 mA / cm 2 or more. of 1 mA / cm 2 of current density at the anode, using, for example, platinum or carbon electrodes, for example graphite.
- the pH of the aqueous phase containing the volatile fatty acids is between 2 and 1 1, preferably between 5.5 and 8.
- the Kolbe reaction providing alkanes is favored, while under alkaline pH conditions it is the oxidative deprotonation of the Hofer-Moest reaction providing alkenes that is favored.
- the AGVs thus carboxylic acids, with short and medium carbon chains must be in the form of carboxylates to be used. This is why a low pH will tend not only to reduce the concentration of volatile fatty acids in the form of anions but also the solubility of carboxylic acids or AGV medium carbon chain.
- the pH can be adjusted, inter alia, with sodium hydroxide to maintain high carboxylate concentrations to be subjected to electrolysis. In general, there is no need to use organic solvents, the fermentation media being good electrolytes for the electrosynthesis step 13.
- Organic solvents are necessary almost exclusively for the reagents poorly soluble in water, such as carboxylic acids or AGV with long carbon chains.
- carboxylic acids or AGV with long carbon chains such as carboxylic acids or AGV with long carbon chains.
- methanol, ethanol and isopropanol may be solvents of choice.
- these carboxylic acids or AGV with long carbon chains can be easily separated and concentrated in order to undergo the electrolysis step in a second step and lead to high yields of electrolytic products.
- the products formed respectively at the anode and at the cathode can be easily separated.
- all the compounds obtained by electrosynthesis can be recovered in a single container and separated or transformed thereafter.
- gaseous products 15 formed at the end of the electrosynthesis 13 such as hydrogen, carbon dioxide, alkanes, alkenes can be, by way of non-limiting example, compressed and separated by gas liquefaction. as previously indicated under reference 8.
- the products 14 obtained at the end of this electrochemical conversion step are, among others, mixtures of hydrocarbons, hydrogen and carbon dioxide which contain no contaminant relative to, among others, , natural gas from the oil industry.
- step 13 the non-transformed AGV residues 16 partially leave in step 6 to be extracted (step 9) and / or undergo a new electrosynthesis (step 13).
- Part of the residues 16 is recycled to step 17, namely gasified, incinerated or converted.
- Fermentative metabolites such as volatile fatty acids and residual substrates resulting from the different fermentation, extracting, or electrosynthesis stages, are methanized (step 17) to produce fertilizers and amendments, grouped under reference 18 and biogas.
- This methanation step 17 is, according to an industrial ecology approach, also applied to a fraction of unfermented residues or substrates.
- we produce energy and heat typically by cogeneration. This production of energy and heat is, at least in part, used to cover the energy requirements of the process.
- the process of the invention makes it possible to produce, advantageously continuously, and with a high yield of the carbon-based molecules with a minimum loss of initial organic carbon.
- Example 1 Discontinuous fermentation of slaughterhouse by-products in a non-sterile bioreactor mode
- a 5L volume fermenter or bioreactor of useful volume containing an anaerobic culture medium 0.5 g / LK 2 HPO 4, 0.5 g / L KH 2 PO 4, 1.0 g / L MgSO 4, 0.1 g / L LCaCI2, 1 ml Hemin and 5 ml vitamin
- anaerobic culture medium 0.5 g / LK 2 HPO 4, 0.5 g / L KH 2 PO 4, 1.0 g / L MgSO 4, 0.1 g / L LCaCI2, 1 ml Hemin and 5 ml vitamin
- anaerobic culture medium 0.5 g / LK 2 HPO 4, 0.5 g / L KH 2 PO 4, 1.0 g / L MgSO 4, 0.1 g / L LCaCI2, 1 ml Hemin and 5 ml vitamin
- a mixture of non-sterilized slaughterhouse waste blood, viscera, stercorals, meat waste, in ratio 1/1/1 / 2
- Example 2 Semi-continuous fermentation of organic fractions of household waste bioreactor non-sterile mode.
- Example 1 is repeated with the same culture medium but using a substrate composed of the fermentable fraction of the household waste at a concentration of 50 g / L dry matter instead of slaughterhouse waste.
- extractions are carried out on the medium during fermentation.
- the fermentation takes place over 2000 hours and several in situ extraction sequences are carried out in the bioreactor.
- the extraction is of the liquid-liquid type, it being understood that the volatile fatty acids are always produced in the liquid phase and that the solvent used for this example is pentane.
- the extraction can be carried out without irreversible constraints directly in the fermentation reactor 4. It is possible to carry out a continuous fermentation with the extraction of the metabolites. fermentation inhibitors, that is, by extracting the volatile fatty acids responsible for the acidosis of the medium as they are produced. Alternatively, these extraction operations may be performed in a second compartment, the latter compartment being able to be located in the bioreactor 4.
- a solution of 1M sodium acetate was subjected to an electrolysis reaction using graphite electrodes with a current density of 100 mA / cm 2 .
- the metabolites obtained in the gas phase are hydrogen (350 ml or 15 mmol), carbon dioxide (330 ml or 13.8 mmolC), methane (7 ml or 0.3 mmolC) and ethane ( 30 ml or 2.51 mmolC).
- the metabolites obtained in the liquid phase are methyl acetate (66 mg or 0.9 mmol) and methanol (87 mg or 2.7 mmol).
- the Cmol (Cmol.Product / Cmol.Substrate) balance of this reaction is 0.9 ⁇ 0.1.
- the yields of hydrogen, carbon dioxide, ethane, methane, methyl acetate and methanol are respectively 473 ml / g of acetate, 446 ml / g of acetate, 41 ml / g of acetate, 10 ml / g acetate, 90 mg / g acetate and 1 18 mg / g acetate.
- Example B
- Example A is repeated but with 1M sodium propionate as the substrate. After 180 minutes, 56% of the initial propionate concentration was consumed. Hydrogen, methane, carbon dioxide, ethene and butane are obtained in the gas phase and ethanol and ethyl propionate are obtained in the liquid phase.
- the amidation reaction is carried out in a reflux assembly from a mixture of a biosourced acetic acid solution and an ammonia solution under conditions stoichiometric.
- the reaction mixture is heated at 80 ° C for 4 hours and then the excess reagents are distilled off.
- the product of the reaction is recrystallized in order to obtain the biosourced acetamide.
- the yield of the amidation reaction under these conditions is 63%.
- Example C is repeated, but with a biosourced butyric acid solution and at a temperature of 90 ° C. After 5 hours and after crystallization of the biobased butyramide, the yield of the amidation reaction was 69%.
- Example C is repeated with a mixture of biosourced volatile fatty acids (acetic acid, propionic acid, butyric acid, isobutyric acid, isovaleric acid, valeric acid, isocaproic acid, caproic acid, heptanoic acid, octanoic acid, etc.) derived from the extraction phase as described in the previous examples at a temperature of 85 ° C. After 6 hours, after removal of excess reagents by distillation and after recrystallization of the biosourced amides, the yield of the amidation reaction is 74%.
- biosourced volatile fatty acids acetic acid, propionic acid, butyric acid, isobutyric acid, isovaleric acid, valeric acid, isocaproic acid, caproic acid, heptanoic acid, octanoic acid, etc.
- the biosourced amides obtained are the amides corresponding to the biosourced carboxylic acids present in the mixture (acetamide, propanamide, isobutyramide, butyramide, isovaleramide, valeramide, isohexanamide, hexanamide, heptanamide and octanamide, etc.).
- amidation reactions which make it possible to produce bio-sourced amides from biosourced volatile fatty acids can also be carried out with substituted amines in order to obtain secondary and tertiary amides.
- Example F Esterification of a mixture of AGV
- an equimolar mixture of biosourced volatile fatty acids obtained after fermentation and extraction (acetic acid, propionic acid, butyric acid, isobutyric acid, isovaleric acid, valeric acid, isocaproic acid, caproic acid, heptanoic acid, octanoic acid, phenyl acetic acid, phenyl propionic acid) (2 mL) ) and ethanol (1. 51 mL) is refluxed for 1 h15.
- Sulfuric acid (54 ⁇ ) is initially added to the reaction medium as a catalyst.
- phase chromatography gaseous ethyl esters corresponding to the acids present in the initial mixture that is to say in the example: ethyl acetate, ethyl propionate, ethyl isobutyrate, ethyl butyrate , ethyl isopentanoate, ethyl pentanoate, ethyl isohexanoate, ethyl hexanoate, ethyl heptanoate, ethyl octanoate, phenylacetate, ethyl and ethyl phenylpropionate.
- a conversion yield of 69% of the carboxylic acids to esters is obtained.
- fermentative metabolites such as AGV, namely according to Examples A to F and in a non-limiting manner, acetic, propionic, butyric, isobutyric, isovaleric, valeric, isocaproic, caproic, heptanoic, octanoic, phenyl acetic, phenylpropionic acid are easily used as precursors of final molecules of economic and energetic interest, it being understood that these metabolites are produced by fermentation.
- the implementation of such a process involves not only the presence in the installation of at least one fermentation reactor but also at least one extraction member, adapted to implement the extraction step 9 and at the same time.
- least one synthesis member adapted to implement the electrosynthesis step 13 or, alternatively, another chemical step.
- Such an installation advantageously comprises storage members of the substrate 1 and / or products from the extraction and / or electrosynthesis and other chemical synthesis stages.
- Management and control means such as temperature sensors, pH probes, are provided.
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FR1457198A FR3024159B1 (fr) | 2014-07-25 | 2014-07-25 | Procede de production de molecules a partir de biomasse fermentescible |
PCT/FR2015/051967 WO2016012701A1 (fr) | 2014-07-25 | 2015-07-17 | Procédé de production de molécules organiques à partir de biomasse fermentescible |
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FR3072971B1 (fr) | 2017-10-26 | 2021-01-08 | Veolia Environnement Ve | Procede de fermentation acidogene pour la production d'acides organiques de 2 a au moins 5 atomes de carbone et installation correspondante |
FR3074174B1 (fr) | 2017-11-30 | 2020-02-07 | Afyren | Procede de valorisation de sels de potassium coproduits de procedes de fermentation |
FR3075222B1 (fr) | 2017-12-19 | 2022-03-11 | Afyren | Vinasse comme milieu de fermentation |
FR3087449A1 (fr) | 2018-10-19 | 2020-04-24 | Afyren | Procede de preparation de molecules organiques par fermentation anaerobie |
FR3127229A1 (fr) * | 2021-06-04 | 2023-03-24 | Bio-Think | Procédé de production d’esters d’acides gras volatils, lesdits esters étant utilisés comme solvant d’extraction |
EP4202051A1 (fr) | 2021-12-23 | 2023-06-28 | Fundación Centro Gallego de Investigaciones del Agua | Procédé et système d'obtention d'acides gras volatils de grande pureté |
CN114634953B (zh) * | 2022-02-14 | 2024-04-16 | 中国科学院广州能源研究所 | 一种有机垃圾处理方法及其能源化利用系统 |
CN114806858A (zh) * | 2022-05-25 | 2022-07-29 | 清研环境科技股份有限公司 | 回收厌氧发酵体系中挥发性脂肪酸的装置及方法 |
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US4358537A (en) * | 1980-10-22 | 1982-11-09 | Institute Of Gas Technology | In situ biological beneficiation of peat in the production of hydrocarbon fuels |
US5807722A (en) * | 1992-10-30 | 1998-09-15 | Bioengineering Resources, Inc. | Biological production of acetic acid from waste gases with Clostridium ljungdahlii |
US6043392A (en) * | 1997-06-30 | 2000-03-28 | Texas A&M University System | Method for conversion of biomass to chemicals and fuels |
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WO2013033772A1 (fr) * | 2011-09-06 | 2013-03-14 | Anaeco Limited | Méthode de régulation de procédé |
US20130309740A1 (en) * | 2011-11-22 | 2013-11-21 | Washington State University Research Foundation | Two-Stage Anaerobic Digestion Systems Wherein One of the Stages Comprises a Two-Phase System |
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BR112017001232A2 (pt) | 2017-11-28 |
AU2015293776B2 (en) | 2019-05-16 |
FR3024159A1 (fr) | 2016-01-29 |
FR3024159B1 (fr) | 2018-02-02 |
CA2955770A1 (fr) | 2016-01-28 |
US20170158572A1 (en) | 2017-06-08 |
AU2015293776A1 (en) | 2017-02-16 |
BR112017001232B1 (pt) | 2023-03-14 |
CA2955770C (fr) | 2023-08-29 |
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CN106536741A (zh) | 2017-03-22 |
RU2017101975A3 (fr) | 2018-12-24 |
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