WO2022248797A1 - Reacteur bio-electrochimique optimise, notamment pour la degradation de la demande chimique en oxygene d'un effluent - Google Patents
Reacteur bio-electrochimique optimise, notamment pour la degradation de la demande chimique en oxygene d'un effluent Download PDFInfo
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- WO2022248797A1 WO2022248797A1 PCT/FR2022/050969 FR2022050969W WO2022248797A1 WO 2022248797 A1 WO2022248797 A1 WO 2022248797A1 FR 2022050969 W FR2022050969 W FR 2022050969W WO 2022248797 A1 WO2022248797 A1 WO 2022248797A1
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- effluent
- support material
- bio
- microbial biofilm
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title description 4
- 230000015556 catabolic process Effects 0.000 title description 4
- 238000006731 degradation reaction Methods 0.000 title description 4
- 239000001301 oxygen Substances 0.000 title description 4
- 229910052760 oxygen Inorganic materials 0.000 title description 4
- 239000000126 substance Substances 0.000 title description 4
- 239000000463 material Substances 0.000 claims abstract description 114
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- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 claims description 2
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- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/005—Combined electrochemical biological processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M25/00—Means for supporting, enclosing or fixing the microorganisms, e.g. immunocoatings
- C12M25/16—Particles; Beads; Granular material; Encapsulation
-
- 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
- C12M35/00—Means for application of stress for stimulating the growth of microorganisms or the generation of fermentation or metabolic products; Means for electroporation or cell fusion
- C12M35/02—Electrical or electromagnetic means, e.g. for electroporation or for cell fusion
-
- 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
- C12P3/00—Preparation of elements or inorganic compounds except carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
- C12P5/02—Preparation of hydrocarbons or halogenated hydrocarbons acyclic
- C12P5/023—Methane
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
-
- 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
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/02—Hydrogen or oxygen
-
- 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
- C25B3/01—Products
- C25B3/03—Acyclic or carbocyclic hydrocarbons
-
- 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
- C25B3/01—Products
- C25B3/07—Oxygen containing compounds
-
- 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
- C25B3/20—Processes
- C25B3/25—Reduction
-
- 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
- C25B3/20—Processes
- C25B3/25—Reduction
- C25B3/26—Reduction of carbon dioxide
-
- 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
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/13—Single electrolytic cells with circulation of an electrolyte
-
- 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
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/40—Cells or assemblies of cells comprising electrodes made of particles; Assemblies of constructional parts thereof
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/16—Biochemical fuel cells, i.e. cells in which microorganisms function as catalysts
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46109—Electrodes
- C02F2001/46152—Electrodes characterised by the shape or form
Definitions
- the innovation relates to the field of treatment and recovery of effluents containing biodegradable organic pollution, such as wastewater (municipal or industrial) or organic waste such as slurry or leachate, and more particularly electrochemical systems and processes.
- bio-electrochemical reactors that is to say electrochemical devices of which at least one of the electrodes, called bio-electrode, is in contact with microorganisms.
- Such electrochemical systems and processes which are relatively recent technologies (approximately 20 years old) allow in particular the coupling of the treatment of effluents containing organic matter (waste water, hydrolyzate, etc.) with the production of electrical energy or value-added molecules, such as organic acids and/or alcohols.
- organic matter waste water, hydrolyzate, etc.
- electrical energy or value-added molecules such as organic acids and/or alcohols.
- microbial fuel cells we talk about microbial fuel cells
- microbial electrolysers we talk about microbial electrolysers.
- microorganisms generally in the form of a biofilm.
- the use of microorganisms generates constraints such as the instability of biological activity over time, the aging of the biofilm in connection with the accumulation of biomass, sensitivity to certain inhibitors, including dioxygen (O2) in certain cases.
- O2 dioxygen
- a first solution consists in using brush-shaped electrodes facilitating the ladder climb, the establishment of a biofilm as well as the maintenance of the bio-electrochemical system.
- these brush-shaped electrodes develop more surface area than planar electrodes.
- this advantage is quickly offset when the brushes become clogged with microbial biofilms.
- This configuration therefore also suffers from low electrode surface/volume of the anode compartment ratios.
- Another family of solutions is inspired by wastewater treatment processes using fixed or granular biomass. These solutions use fixed-bed granular electrodes, the electrodes forming compartments either completely filled with granular material, as described for example by Zhou, Y. et al.
- Jia, Y.H. et al. [2] described a microbial electrolysis cell for producing hydrogen gas from biomass by a process catalyzed by microorganisms.
- the bioreactor used comprises an anode compartment and a cathode compartment separated by a membrane, the anode compartment comprising modules forming metal baskets filled with graphite granules on which the microorganisms are deposited. These modules are arranged vertically, side by side horizontally, parallel to each other with spacing.
- the flow of the effluent to be treated is thus preferentially along the modules, and not through them, which does not favor exchanges with the graphite granules and the microorganisms.
- the granules located inside the baskets cannot be fluidized.
- the reactor is formed of a tubular cation exchange membrane.
- the anode is a carbon fabric supported by a metal mesh arranged inside the tubular membrane, along the internal wall of the latter.
- the interior of the tubular membrane includes membranes in the form of hollow fibers and particles of activated carbon.
- the cathode is formed of a carbon fabric covered with Pt/C powder surrounding the tubular membrane.
- microorganisms are introduced inside the tubular membrane.
- the activated carbon particles located inside the tubular membrane are fluidized.
- MFC microbial fuel cell
- Liu J et al. [4] described a microbial electrolysis cell with fluidized granular electrode operating in batch.
- the reactor is in the form of a PVC tube (polyvinyl chloride) comprising particles of activated carbon as a fluidized anode, these particles will serve as a support for the microorganisms.
- a nylon filter positioned at the bottom of the reactor prevents particles from leaving the reactor from below.
- the anode current collector is made of a block of graphite positioned inside the reactor in its lower half.
- the cathode is made of a cylindrical metal mesh positioned in the upper part of the reactor.
- a recirculation loop connects the reactor outlet to an inlet.
- the effluent circulates from bottom to top and fluidizes the activated carbon particles which are discharged onto the anode current collector. During fluidization, however, these particles are likely to be carried as far as the cathode, which would disrupt the operation of the process. In addition, batch operation is not suitable for an industrial scale.
- the article Liu, J. et al. [5] describes a microbial electrolysis cell comprising two chambers arranged one above the other and separated by a titanium grid acting as an anode current collector.
- the lower chamber forms an anode chamber which contains activated carbon granules intended to receive the microorganisms
- the upper chamber forms a cathode chamber.
- a magnetic stirrer makes it possible to fluidize the activated carbon granules inside the anode chamber. This system also works in batch, which is not very suitable for an industrial scale.
- the systems of the prior art aim to maximize the faradic yield and/or the production of molecules of interest (such as acetate, lactate, etc..., biorefinery).
- molecules of interest such as acetate, lactate, etc..., biorefinery
- the present invention pursues a different objective: it proposes a bioelectrochemical system which optimizes the degradation of organic molecules, in particular with a view to applications at the industrial stage.
- the invention therefore aims to overcome the drawbacks of the prior art by proposing a bio-electrochemical reactor - in particular an electrolysis or microbial electrosynthesis reactor - capable of treating an effluent containing organic pollution (biodegradable organic matter), such as wastewater effluent, suitable for industrial scale.
- a bio-electrochemical reactor in particular an electrolysis or microbial electrosynthesis reactor - capable of treating an effluent containing organic pollution (biodegradable organic matter), such as wastewater effluent, suitable for industrial scale.
- the invention also aims to provide a process for the treatment or pre-treatment of an effluent containing in particular organic pollution (biodegradable organic matter) comprising a step of bio-electrochemical reaction.
- the system and the method of the invention are energy efficient, and competitive with respect to treatment using an aeration tank both in terms of COD reduction (Chemical Oxygen Demand ) and energy consumption.
- the present invention relates to a bio-electrochemical reactor for treating a liquid effluent, comprising at least one anode compartment and at least one cathode compartment.
- at least one of the anode and cathode compartments is a microbial biofilm compartment comprising: at least one fluid inlet located at one end of the compartment, at least one fluid outlet located at an opposite end of the compartment, means for circulating the fluid inside the compartment between the at least one inlet and the at least one outlet along an X direction, an electrolyte comprising electro-active microorganisms, a biocompatible granular support material, a multi-stage current collector located between the at least one inlet and the at least one fluid outlet of said compartment with microbial biofilm, said collector comprising at least two stages each defining a chamber acting as a container for the granular support material and allowing
- the direction X of circulation of the fluid inside the compartment is non-parallel, and preferably orthogonal, or substantially orthogonal, to a direction Z going from the anode compartment to the cathode compartment.
- This direction X can advantageously be parallel to the direction of gravity to facilitate fluidization.
- the chambers of the current collector are then positioned one above the other.
- the current collector matches the shape of the microbial biofilm compartment over the height of said collector measured in the X direction.
- each chamber of a stage of the current collector has a section which extends over the entire surface of an internal section of the microbial biofilm compartment, these sections being defined in a plane perpendicular to the direction X.
- each chamber conforms to the shape of the microbial biofilm compartment.
- the effluent to be treated circulates inside the microbial biofilm compartment, it passes through the granular support material of each chamber of a stage of the current collector over the entire surface of the internal section of the microbial biofilm compartment.
- a height at rest of granular support material measured along the direction X in the absence of fluid circulation inside the compartment at microbial biofilm is suitable for fluidization of said granular support material.
- This height at rest is less than the total height of the chamber.
- This fluidization is obtained by the circulation of the effluent to be treated (possibly supplemented by the circulation of a fluidization gas) by the circulation means with a flow rate greater than or equal to a minimum flow rate for fluidization of the support material.
- granular content inside the current collector are circulation means at a rate greater than or equal to a minimum fluidization rate of the granular support material contained inside the current collector.
- microbial film compartment(s) comprises(comprises) one or more stages of fluidized material (when the effluent circulates) provides a good compromise between the treatment capacity and quality of the reactor and its electrochemical performance.
- This particular arrangement makes it possible in particular to improve the contact between the electro-active microorganisms by maximizing the attachment surface for the microorganisms, in particular compared to systems equipped with non-fluidized granular electrodes. In this way, the treatment of the effluent can be improved.
- the multi-stage structure of the current collector makes it possible to facilitate and homogenize the fluidization of the granular support material at the level of each fluidized stage. It is thus possible to obtain relatively homogeneous fluidization over all of the fluidized stages, in other words over the entire volume of the compartment occupied by these stages and in particular over the entire height and/or volume of the current collector when the floors are distributed over the entire height and/or volume of the latter. This minimizes dead volumes in the microbial biofilm compartment and clogging, also improving effluent treatment.
- the fluidization takes place along a direction X which is not parallel, and preferably orthogonal to a direction connecting the anode and cathode compartments.
- This characteristic added to the relatively homogeneous fluidization over the entire height and/or the volume of the compartment occupied by the fluidization stages, makes it possible in particular to stabilize the streamlines in the reactor. Fluidization also makes it possible, through friction effects, to moderate the formation of the biofilm, and therefore the sludge generated during the operation of the reactor.
- the reactor and the process of the invention thus make it possible to limit the size of the biological aggregates produced during the treatment of the effluent, which limits the accumulation of materials in the reactor and constitutes a significant advantage in a process for the treatment of an effluent. Moderating biofilm formation also makes it possible to make the most of the potential capacitive properties of the granular support material.
- fluidization makes it possible to limit the apparent growth yields of microorganisms without however altering their activity.
- the multi-stage structure of the current collector also allows great flexibility in the operation and maintenance of the reactor. It is indeed possible to replace the granular support material of a stage independently of the other stage(s). We can then speak of differential renewal of the granular material for each stage.
- the current collector may be formed of a structure in a single part, each chamber being for example equipped with a door for loading the support material, or else, the current collector may be formed of a structure in several parts, for example in several modules electrically connected to each other, each module defining a chamber equipped with a door or having an upper opening open to the material of a basket. For easy handling, the current collector or each module of the current collector can be removable.
- support materials and/or consortia of different microorganisms for each stage. This makes it possible to adapt the support material (material, size, number, density, etc.) and/or the populations of microorganisms according to the objectives sought. This flexibility makes it possible to consider the specialization of the stages in a particular treatment. In particular, it is possible to provide populations of microorganisms specialized in aerobic treatments for the stage closest to the effluent inlet, the microorganisms taking advantage of the traces of oxygen dissolved in the effluent (for example specialized for the oxidation of COD by GO 2 dissolved in the effluent). The following floors would be specialized in anaerobic treatments. The aerobic “chamber” can also be used to protect chambers located downstream which must be strictly anaerobic for the proper development of electro-active microorganisms.
- the electro-active microorganisms can thus be aerobic or anaerobic microorganisms. These microorganisms differ according to the electrode on which they develop as a biofilm, and the characteristics of the electrolyte in which they are immersed. For example, when wastewater or bio-waste hydrolysates are injected into an anodic electrolyte, an abundant population affiliated with the genus Geobacter is observed. On the other hand, in a saline environment, other genera such as Geoalkalibacter or Desulforomonas can become dominant.
- the at least one microbial biofilm compartment may include one or more circuits for recycling the treated effluent.
- This compartment can thus comprise at least one recycling circuit connecting the at least one outlet to the at least one fluid inlet or connecting the at least one outlet to at least one recycling inlet opening into one of the chambers or upstream of one of the chambers with respect to the circulation of the fluid. This can make it possible to facilitate the fluidization of the support material and to increase the residence time of the effluent in the compartment.
- the treated effluent (leaving the microbial biofilm compartment) is returned to one of the fluidization chambers, it is possible to carry out this return to a chamber other than that or those first receiving the effluent to be treated.
- the recycled treated effluent can be returned to a stage situated downstream (relative to the circulation of the effluent) of at least a first stage into which the effluent to be treated enters. This can be particularly advantageous, especially in addition to the specialization of the different chambers.
- the at least one microbial biofilm compartment of the reactor according to the invention may comprise means for introducing a fluidization gas, for example located upstream of a fluidization chamber, in particular upstream of the fluidization chamber furthest upstream with respect to the circulation of the fluid, for example at one of the ends of the compartment, when the fluidization gas and the effluent to be treated circulate in co-current.
- a fluidization gas for example located upstream of a fluidization chamber, in particular upstream of the fluidization chamber furthest upstream with respect to the circulation of the fluid, for example at one of the ends of the compartment
- This introduction can then be carried out downstream of at least one chamber of the non-fluidized current collector
- the introduction of such a gas, circulating in co-current or against the current of the effluent to be treated can facilitate the fluidization granular carrier material within the fluidization chamber(s).
- the anode compartment can be a microbial biofilm compartment, and optionally the cathode compartment can be a microbial biofilm compartment.
- the bio-electrochemical reactor can be: a reactor of which only the anode compartment is a microbial biofilm compartment, for example used, in particular in a bio anode/abiotic cathode configuration, to couple the treatment of material organic matter of an effluent in the anode compartment (by bio-electrochemical oxidation of the COD), either with the production of hh from hhO at the cathode in the case of a microbial electrolysis process, or with a reduction of C> 2 at the cathode for a microbial cell, a reactor of which only the cathode compartment is with a microbial biofilm, for example used in an abiotic anode/bio-cathode configuration, to couple, in the context of electrolysis, a biologically catalyzed reduction (for example denitrification of an effluent or electrosynthesis reaction) in the cathode compartment to an oxidation of H 2 O in the anode
- this type of reactor can be used in bio-electrosynthesis processes coupling treatment of the effluent at the anode and synthesis of carbonaceous molecules at the cathode.
- this type of reactor can be used to couple treatment of the effluent at the anode with denitrification treatment at the cathode of the same effluent or of another effluent.
- microbial biofilm compartment is thus meant a compartment whose electrode is catalyzed by microorganisms, in other words whose electrode is a bio-electrode immersed in an electrolyte comprising electro-active microorganisms.
- the bio-electrode here is a granular electrode.
- the latter is preferably as described in the present invention and comprises in particular a multi-stage current collector as described in the present invention.
- a “bio-electrode” (“bio-anode” or “bio-cathode”) is an electrode covered at least in part with a bacterial biofilm comprising electro-active organisms, i.e. that is to say covered at least on part of its surface immersed in the electrolyte by a bacterial biofilm.
- the entire submerged surface of the bio-electrode is covered with biofilm.
- only part of the surface of the bio-electrode is covered with biofilm.
- the surface covered with biofilm is sufficient to generate the desired activity, in particular in the case of oxidation of hydrolysates of organic waste or of bio-electrochemical synthesis.
- a bio-electrode can be conditioned by introducing an inoculum into the electrolyte or by enriching the effluent to be treated with microorganisms of interest.
- the microorganisms of interest are the microorganisms responsible for bio-electrosynthesis, bio cathodic denitrification or bio-electrochemical oxidation of COD. They include, for example, bacteria capable of using the electrons or hydrogen generated at the cathode to synthesize the desired compounds (such as organic acids or alcohols).
- the inoculum can be prepared from a sludge from anaerobic digester, possibly having undergone a pre-treatment aimed at inactivating methanogenic microorganisms.
- this digester sludge can undergo a heat treatment at a temperature and for a time sufficient to inactivate the methanogenic microorganisms.
- the pretreatment can also include the enrichment of the waste in microorganisms of interest. This step may in particular include the addition of hydrogen and carbon dioxide, for example in a closed flask in discontinuous mode. The culture resulting from this enrichment can be used directly and introduced into the cathode compartment when the reactor is started.
- the reactor according to the invention can be used as a microbial fuel cell to produce electric current.
- the reactor can be an electrolysis reactor or a microbial electrosynthesis reactor comprising means for applying a potential difference between the current collector of the microbial biofilm compartment and the electrode of the other compartment. It can then be used to produce dihydrogen (hh) or chemical molecules of interest (methane, organic acids, alcohol, etc.).
- the cathode compartment with microbial biofilm may comprise at least one other inlet for a carbon source, typically injected in the form of gas, such as CO2, biogas, or syngas, and/or introduced into solution in the form of organic carbon: for example acetate and/or in the form of mineral carbon, in particular a bicarbonate.
- a carbon source typically injected in the form of gas, such as CO2, biogas, or syngas, and/or introduced into solution in the form of organic carbon: for example acetate and/or in the form of mineral carbon, in particular a bicarbonate.
- the bio-electrochemical reactor according to the invention may comprise at least one separator located between the at least one anode compartment and the at least one cathode compartment, for example when soluble molecules are produced, typically at the cathode.
- the separator allows the passage of ions (anions or cations) between the anode and cathode compartments. It may comprise one or more ion exchange membranes, a porous ceramic material allowing the passage of ions, or other.
- the person skilled in the art may in particular choose the separator according to the electrochemical reaction implemented.
- the separator When the separator has two ion exchange membranes, it can also include an inter-membrane compartment.
- This type of separator can be used for any application of the bio-electrochemical reactor of the present invention, but depending on the uses, other types of separators can be used.
- the cathode can advantageously have an active surface greater than the total active surface of the bio-anode. This makes it possible to stabilize the operation of the reactor, as described in document W02020/053529.
- active surface of a bio-electrode here bio-anode or bio-cathode
- bio-anode or bio-cathode is meant the surface exposed to the electrolyte, this surface being polarized.
- the cathode is a bio-cathode
- the reactor also comprises a cathode compartment with a microbial biofilm
- the bio-cathode has greater inertia due to an active surface greater than the total active surface of the bio-anode, which makes it possible to guarantee a particularly stable cathode potential.
- the great stability of the potential of the cathode makes it possible in practice to better control the anode potential by varying the potential difference between the bio-cathode and the bio-anodes, and without having to resort to a reference electrode .
- Such a system thus allows fine control of the anodic potential and therefore optimization of the activity of the anodic biofilm.
- the separator may comprise a cation exchange membrane and an anion exchange membrane separated from each other by an inter-membrane compartment comprising a device for withdrawing molecules synthesized within said reactor.
- the inter-membrane compartment is thus able to collect the ions or molecules produced in the anode and/or cathode compartments.
- the molecules recovered at the level of this inter-membrane compartment can be, for example, ammonium salts, phosphate salts or others. In general, molecules (typically soluble molecules) are recovered at this compartment when the reactor is an electrosynthesis reactor for the synthesis of molecules of interest.
- the membranes can be positioned so that the anode compartment is separated from the cathode compartment by, going from the anode compartment towards the cathode compartment, said cation exchange membrane and said anions.
- cations eg NhV
- anions eg carboxylate ions
- the current collector is advantageously: electrically conductive, and its structure allows the passage of the fluid to be treated but not that of the granular support material.
- the current collector may thus be made of, or contain, a carbon-based material, such as graphite, carbon fiber fabric, etc., or a conductive metal or metal alloy, most often stainless steel, or any other material usually used to make a current collector.
- a carbon-based material such as graphite, carbon fiber fabric, etc.
- a conductive metal or metal alloy most often stainless steel, or any other material usually used to make a current collector.
- the current collector can thus have a structure having a multitude of orifices which do not allow the particulate material to pass (namely the granular support material), preferably formed from a plate perforated, fabric or mesh.
- This type of structure has the advantage of not shielding current lines.
- the dimensions of the orifices will therefore be determined by the dimensions of the particles of granular support material.
- This structure in particular when it is formed of a material that is not very rigid, such as a fabric, can be reinforced by a support, for example of stainless steel, to which the structure is secured.
- the current collector of the microbial biofilm compartment of the reactor according to the invention can extend over 90 to 100% of the height of the microbial biofilm compartment, this height of the microbial biofilm compartment being defined as the distance, in particular the greatest distance, separating the at least one entrance from the at least one exit of the compartment along the direction X.
- the invention is however not limited to this embodiment and a height of the current collector less than 90% of the height of the microbial biofilm compartment could be considered.
- the current collector can match the shape of the microbial biofilm compartment, which makes it possible to further limit, or even eliminate, any dead volume in operation.
- the current collector matches the shape of the microbial biofilm compartment over the entire height of the current collector (measured along the direction X), this height possibly being lower than the height of the microbial biofilm compartment, as explained below. above.
- the current collector can thus occupy 90 to 100% of the interior volume of the microbial biofilm compartment.
- the reactor typically has a parallelepipedic or cylindrical shape.
- the height at rest of the granular support material is adapted to fluidization of the said granular support material.
- a height is less than the height of the fluidization chamber. This height may be determined by calculation and/or experimentation. Typically, this height does not exceed 75%, or even 50% of the height of said fluidization chamber, these heights being measured along the direction X. In other words, the maximum height of granular support material can represent 75%, or even 50% of the total height of the fluidization chamber.
- the minimum height at rest of the granular support will advantageously be non-zero and may be calculated so that the quantity of granular support material is optimal for the formation of a biofilm.
- the height at rest of granular support material inside a fluidization chamber can range from 10 to 75% of the height of the chamber including 10-50% of the chamber height or may be within any range defined by a combination of these limits.
- the total height at rest of granular support material corresponding to the sum of the heights at rest of granular support material in each of the chambers of the current collector of the microbial biofilm compartment may be from 10 to 75% of the total height of the collector of current, in particular from 10 to 50% of the total height of the current collector or included in any range defined by a combination of these limits.
- the sizing of the microbial biofilm compartment and of the current collector in particular when the latter occupies the entire volume of the compartment, can be chosen according to the Di7d ratio with D T the diameter of the fluidized bed (or equivalent diameter if the section of the current collector is not a disc) and d p the average diameter of the granules.
- a homogeneous expansion of the fluidized bed is obtained for a ratio greater than 12 in the ideal case of a cylindrical current collector, of granules of homogeneous and spherical support material.
- the diameter D T obtained for a ratio of 12 thus corresponds to a minimum value of the section of the microbial biofilm compartment.
- the maximum value of this section depends in a manner known to those skilled in the art on the flow rate of the effluent, on the nature of the process, on the residence time.
- this ratio may be from 10 to 15, most often from 12 to 15 in order to limit wall effects.
- the section of the current collector is thus determined, one can choose a height/section ratio of the relevant current collector according to the residence time required to treat a given effluent by a given process, the quantity of granular support material , biological kinetics implemented.
- the choice of the height of the current collector can also be constrained by the pressure drop and the need to fluidize the granules of the granular support material in all the fluidization chambers.
- the person skilled in the art will be able to determine the dimensions of the microbial biofilm compartment by calculation and/or experimentation. It will thus be noted that the current collector has, over its entire height, a section identical to an internal section of the microbial biofilm compartment. In other words, the section of the current collector extends over the entire surface of the internal section of the microbial biofilm compartment.
- the height of each fluidization chamber measured along direction X can be adapted for optimal fluidization.
- This height can in particular be determined according to characteristic parameters of the granular support material such as density, geometry and size of the particles of the granular support material and at least one parameter characteristic of the circulation of the fluid (effluent) inside the compartment. to microbial biofilm, such as its superficial velocity.
- characteristic parameters of the granular support material such as density, geometry and size of the particles of the granular support material and at least one parameter characteristic of the circulation of the fluid (effluent) inside the compartment.
- microbial biofilm such as its superficial velocity.
- biocompatible granular support material is meant a support material in granular form (which is in the form of particles or granules) and on which microorganisms can grow.
- the granular support material may be an electrically conductive material, so as to exhibit capacitive effects, such as granular graphite, granular activated carbon (GAC), biochar or magnetite or else a composite material exhibiting an outer conductive layer.
- a composite material can have a core made of a very sparse material covered with a conductive coating, which can make it possible to obtain a support material that is less dense than the fluid to be treated.
- the granular support material can be an electrically non-conductive material, for example a polymer material such as polyethylene. The capacitive effect is then based on that of the biofilm formed.
- biocompatible granular support material is meant a support material in granular form (which is in the form of particles or granules) and on which microorganisms can grow.
- the granular support material can advantageously be porous, so as to present a large (apparent) surface, to maximize the possibilities of attachment of microorganisms. It will be possible to use a granular support material having pores with a diameter of 1 to 100 ⁇ m, typically from 10 to 100 ⁇ m.
- the pore size distribution can be determined by nitrogen volumetry from adsorption isotherms recorded at 77 K by applying methods well known to those skilled in the art (Barett, EP; Joyner, LG; Halenda, PPJ Am. Chem. Soc. 1951, 73, 373-380).
- the choice of the granular support material, and in particular of its pore distribution, its pore volume and/or its specific surface area, is made by testing with conventional techniques known to those skilled in the art and depends on the nature of the microorganisms. of interest.
- a granular support material with a particle size less than or equal to 2 cm, or even 1 cm, for example from 0.2 to 2 mm, in particular equal to 2 mm or comprised within any range defined by a combination of these limits.
- the particle size is the statistical distribution of the size of the granules. It can be measured by sieving or by laser diffraction.
- the density of the granular support material can be chosen according to the direction of fluidization, ascending or descending, in other words according to the difference in density between the effluent to be treated and the support material. Since the effluent to be treated most often comprises 50 vol% or more of water, it may be considered, depending on the case, that the density of the effluent is equal to that of water or close to that of water.
- the granular support material may for example have a density greater than that of water, in particular greater than 1000 kg/m 3 , advantageously less than or equal to 3000 kg/m 3 , for example from 1100 kg/m 3 to 2500 kg/m 3 or within any range defined by a combination of these limits. In this case, the flow of fluid used to fluidize the support material will be upward to fluidize the granules.
- the granular support material may have a density less than that of water, in particular less than 1000 kg/m 3 , for example from 100 to 900 kg/m 3 or in any range defined by a combination of these limits. In this case, In this case, the flow of fluid used to fluidize the support material will be downward to fluidize the granules.
- the density of the granular support material can be measured by weighing in a pycnometer.
- the reactor can also comprise means for regulating the pH, the temperature, and/or the level of electrolyte, preferably, in each of the anode and cathode compartments.
- the reactor according to the invention may comprise a structure of the multistack type, with a (horizontal) succession of an anode compartment, a first intermembrane compartment, a cathode compartment, a second intermembrane compartment, it being understood that one end of this succession is one anode, and the other is a cathode.
- the invention also relates to a method for treating a liquid effluent implementing a bio-electrochemical reactor according to the invention under conditions making it possible to fluidize the granular support material present in one or more chambers of the current collector.
- this fluidization can be obtained by the circulation of the effluent to be treated, possibly supplemented by the circulation of a fluidization gas introduced for this purpose into the reactor.
- This fluidization gas can be an inert gas with respect to the bio-electrochemical reactions involved or participate in these reactions (for example in the case of a cathode compartment with a microbial biofilm of an electrosynthesis reactor in which a carbon source is introduced in the form of a gas).
- the effluent to be treated is introduced inside the at least one microbial biofilm compartment of the bio-electrochemical reactor, and the effluent is circulated, in particular continuously, to treating inside the microbial biofilm compartment with a flow rate greater than or equal to a minimum fluidization flow rate of the granular support material contained inside the current collector.
- the circulation of the effluent to be treated at this flow rate is carried out by the means of circulation of the fluid of the bio-electrochemical reactor of the present invention.
- the effluent is subjected to a step of treatment by a bioelectrochemical reaction catalyzed by the electro-active microorganisms contained in the at least one microbial biofilm compartment and a treated or partially treated effluent is recovered at the outlet of the latter.
- provision may be made to introduce a fluidization gas inside said at least one microbial biofilm compartment upstream of at least one fluidization chamber, for example downstream of a chamber of the current collector, preferably a chamber located in the immediate vicinity of the at least one fluid inlet to be treated inside the compartment.
- recycling of the treated or partially treated effluent may be provided. It will thus be possible to return at least part of the treated or partially treated effluent leaving said at least one microbial biofilm compartment inside said compartment upstream of at least one fluidization chamber, optionally downstream of a chamber of the current collector, preferably a chamber located in the immediate vicinity of the at least one fluid inlet to be treated inside the compartment. Note that it is possible to recycle all or part of the treated effluent or partially treated upstream of one or more fluidization chambers, and downstream of a collector chamber, which then functions as a fixed bed chamber.
- the effluent to be treated then circulates inside the microbial biofilm compartment mixed with the recycling of treated or partially treated effluent with a flow rate greater than or equal to the minimum flow rate for fluidization of the granular support material contained in the inside the current collector.
- the effluent to be treated possibly mixed with the recycled part of the treated or partially treated effluent, forms a continuous liquid phase which will fluidize the granular support material.
- An additional injection of a fluidizing gas contributes to the fluidization of the granular support material.
- this minimum flow rate can be determined from a minimum superficial velocity of fluidization of the fluid used to fluidize the support material, namely the effluent to be treated, alone or mixed with the recycled part of the treated effluent or partially processed.
- This minimum speed is a minimum speed of fluidization of all the particles. When these particles have different sizes, the fluidization of the larger particles will typically be sought.
- superficial velocity we mean the hypothetical flow velocity calculated as if the given phase or fluid were the only one to flow or to be present in a given section of the microbial biofilm compartment.
- the superficial velocity can be defined as the ratio of the volume flow rate of the phase or of the fluid (m 3 /s) on the surface of the section of the reactor (m 2 ). One can thus easily access the fluid flow rate by determining the superficial velocity.
- the minimum superficial fluidization velocity of the support material can be calculated according to the following formula:
- the minimum superficial velocity of fluidization of the support material can be determined. from correlations integrating the fluidization gas injection speeds, such as three-phase co-current correlations (Larachi et al., 2000, Ind. Eng. Chem. Res., 39, 563 - 572) or against the current (Sur et al., 2017, Journal of Environmental Chemical Engineering, 5, 3518-3528).
- the superficial velocity of circulation of the fluid ensuring the fluidization, and consequently its volumetric flow rate will be lower than a speed of entrainment of the particles corresponding to the speed from which the particles of smaller size are entrained.
- the surface speed of circulation of the fluid providing the fluidization, and consequently its volume flow can be lower than a speed called “bubbling speed" corresponding to the speed from which the fluidized bed is no longer homogeneous and where "bubbles" or pockets of effluent will form in the granular bed.
- bubbling speed a speed from which the fluidized bed is no longer homogeneous and where "bubbles" or pockets of effluent will form in the granular bed.
- the direction of circulation of the fluid ensuring the fluidization namely the effluent to be treated alone or mixed with recycling, will be chosen according to the density of the support material.
- the direction X of circulation of the effluent to be treated inside the anode compartment being parallel to the direction of gravity, the effluent to be treated, alone or mixed with the recycled part of the treated or partially treated effluent , circulates:
- a fluidization gas used to fluidize the support material, it can circulate either co-current or against the current of the effluent to be treated, the latter case can for example be chosen when the density of the granular support material is less than the density of the effluent to be treated.
- the residence time of the effluent inside the microbial biofilm compartment is from 1 to 48 hours, for example 6 hours or included in any range defined by a combination of these values.
- the use of recycling makes it possible in particular to adjust the residence time of the effluent to be treated to the pollution content to be treated, in particular according to the desired COD abatement rate (in the case of a compartment with anodic microbial biofilm).
- different electro-active microorganisms can be introduced into at least two separate chambers of the current collector of the microbial biofilm compartment.
- a specific granular support material and/or a specific superficial velocity of the effluent to be treated for example to form a fixed or fluidized bed
- the current collector of the microbial biofilm compartment of the reactor when it is an anode compartment, it may have, from upstream to downstream in the direction of circulation of the effluent: at least one stage in which the dioxygen contained in the effluent to oxidize the COD contained therein, one or more stages located downstream operating in anaerobiosis.
- the current collector of the microbial biofilm compartment of the reactor when it is a cathodic compartment (in the case of a microbial cell), it may have, from upstream to downstream according to the direction of circulation of the effluent: at least one GO2 reduction stage, at least one other stage ensuring the denitrification of the effluent to be treated.
- the current collector of the microbial biofilm compartment of the reactor when it is a cathodic compartment (case of a reaction of electrosynthesis), it can present, from upstream to downstream according to the direction of circulation of the effluent, stages corresponding to the various stages of synthesis of a complex molecule such as for example the synthesis of caproic acid.
- stages corresponding to the various stages of synthesis of a complex molecule such as for example the synthesis of caproic acid.
- One can then provide a stage for the reduction of CO2 to acetate, a stage for the reduction of acetate to ethanol and a stage for the production of caproic acid by reduction of ethanol, acetate and CO2 .
- different granular support materials can be used in at least two separate chambers of the current collector of the microbial biofilm compartment, in combination or not with the introduction of different electro-active microorganisms and/or with the choice of specific granular support material and/or of a specific superficial velocity of the effluent to be treated.
- the reactor and the method according to the present invention are useful for the treatment of effluents comprising biodegradable organic matter, such as a waste water effluent or a hydrolyzate of organic waste. It may in particular be sludge or wastewater from treatment plants.
- the effluents comprising biodegradable organic matter used in the invention are typically: slurries, leachates, hydrolysates of bio-waste, hydrolyzed sludge from treatment plants, various organic liquid fractions from treatment plants, water urban waste after primary settling, organic industrial effluents, for example from agro-food industries, digestates from treatment plants, or a mixture of several of these effluents.
- These effluents typically contain more than 50vol% water, generally more than 60vol% water.
- the water content may be at least 95 vol%, or even at least 99 vol%, for example up to 99.9 vol%.
- the water content can be within any range defined by the above limits.
- the remaining percentages are solids, such as particles, suspended solids, colloids, etc.
- the effluent is a waste water effluent, for example organic liquid fractions from treatment plants, urban waste water in particular after primary settling, organic industrial effluents (for example from the food industry), or a mixture of these.
- a waste water effluent for example organic liquid fractions from treatment plants, urban waste water in particular after primary settling, organic industrial effluents (for example from the food industry), or a mixture of these.
- the electrolyte of the microbial biofilm compartment thus contains such organic carbonaceous effluents in liquid form, introduced either raw or diluted in a synthetic base electrolyte.
- the content of organic matter quantified by measuring the COD is advantageously between 0.01 and 200 g/L, preferably between 0.1 and 20 g/L, more preferably between 0.5 and 5 g/L.
- COD is the measure of all oxidizable substances, whether biodegradable or not. COD can be measured according to standard NFT 90-101 -February 2001 or ISO 6060-1989.
- the reactor and the method according to the invention can also be used to carry out a denitrification treatment of an effluent of the aforementioned type.
- the reactor and the process according to the invention can be used for the production by electrosynthesis of organic waste, and in particular by electrosynthesis of one or more of the aforementioned effluents, of dihydrogen or of organic molecules of interest chosen from organic acids, alcohols, methane.
- the reactor and the method according to the invention allow continuous treatment of an effluent to be treated, suitable for an industrial application.
- FIG. 1 schematically represents an embodiment of a bioelectrochemical reactor according to the invention comprising a microbial biofilm compartment.
- FIG. 2 schematically represents another embodiment of a microbial biofilm compartment of a reactor according to the invention.
- FIG. 3 schematically represents yet another embodiment of a microbial biofilm compartment of a reactor according to the invention.
- Figures 4A and 4B schematically represent a first case of fluid circulation through a current collector, respectively without and with fluidization gas.
- Figures 5A and 5B schematically represent a second case of fluid circulation through a current collector, respectively without and with fluidization gas.
- FIG. 1 represents a bio-electrochemical reactor 10 comprising an anode compartment 12 and a cathode compartment 14 separated by a separator 13.
- the anode compartment 12 is a microbial biofilm compartment as defined in the present invention. It thus comprises three inlets 121, 122, 123 for the effluent to be treated, here located at a lower end of the compartment 12 and an outlet 124 for the treated effluent located at an upper end. of the compartment 12.
- Means 125 for circulating the fluid inside the compartment such as a pump, or other, allow the circulation of the fluid in a direction X between the inlets 121-123 and the outlet 124.
- the direction X is here a vertical upward direction, perpendicular to the direction Z, here horizontal, going from the anode compartment 12 to the cathode compartment 14.
- the invention is of course not limited by the number of inlets and/or outlets of the effluent, nor by the nature of the circulation means provided that the effluent to be treated can circulate inside the compartment 12.
- the compartment 12 further comprises a multi-stage current collector 15 electrically connected to a device 16 which may be an electrical component (for example an electrical resistor) for use of the reactor as a fuel cell or a device for applying a voltage for use of the reactor as an electrolysis reactor or an electrosynthesis reactor.
- a device 16 which may be an electrical component (for example an electrical resistor) for use of the reactor as a fuel cell or a device for applying a voltage for use of the reactor as an electrolysis reactor or an electrosynthesis reactor.
- the multi-stage current collector 15 represented comprises 5 stages each defining a chamber 151-155 containing a granular support material 17.
- the multi-stage current collector 15 is for example formed from a grid of conductive material, for example Stainless steel.
- Collector 15 is advantageously removable to facilitate filling of the chambers. It is possible to provide for this purpose an opening for filling each chamber which can be closed by a door or make a modular structure in which each chamber defines a removable container, for example in the form of a basket, which can be inserted/extracted from a support structure, the entire support structure and removable containers being made of conductive material and electrically connected to form the current collector.
- each chamber 151 -155 has a height H c and receives the granular support material 17 over a height H L , at rest, that is to say in the absence of fluid circulation inside the compartment. These heights are measured parallel to the direction X.
- This height H L , at rest corresponds for example to half the height H c to facilitate the fluidization of the support material inside the chambers.
- the current collector 15 extends over the entire height H of the compartment 12 whose shape it matches: its internal volume is therefore substantially identical to the internal volume of the compartment 12, thus limiting the dead volumes.
- each chamber 151-155 extends over the entire surface of the internal section of the compartment 12.
- the current collector 15 thus matches, over its entire height measured in the direction X, the shape of the internal volume of compartment 12. All of the treated effluent thus passes through each chamber.
- the cathode compartment 14 comprises an electrode 18 immersed in an electrolyte circulating inside the compartment between an inlet 141 and an outlet 142, the electrode 18 being electrically connected to the device 16.
- the separator 13 is here in the form of an inter-membrane compartment defined by ion exchange walls 131 and 132.
- one of the membranes 131, 132 is a cation exchange membrane and the other an ion exchange membrane. anions.
- a withdrawal device comprising for example an outlet 133 connected to a pump or the like (not shown) can be provided as shown.
- the invention is not limited by the nature of the cathode compartment, which may be a bio-cathode comprising an electrolyte containing electro-active microorganisms having a structure identical to that of the anode compartment or a structure similar to those existing (granular electrode with fixed bed, with brushes, with plates, etc.).
- the invention is not limited either by the shape of the separator 13 provided that the latter is permeable to the ions which must circulate between the cathode and the anode.
- the circulation of the effluent through the stages of the current collector 15 in the upward direction X makes it possible to fluidize the granular material.
- the latter will thus be distributed in a relatively homogeneous manner inside each chamber, here over the entire height of the compartment 12, allowing the development of a biofilm on most of the granules of the support material 17.
- these granules regularly come into contact with the current collector, thus making it possible to discharge.
- FIG. 2 shows a microbial biofilm compartment 212 similar to that described with reference to Figure 1 but including a recycling circuit.
- the compartment 212 comprises a multi-stage current collector comprising here three stages E1 to E3 each defining a chamber intended to receive the support material (not represented). As seen in this figure, the section of each chamber extends over the entire surface of the internal section of the compartment 212.
- the effluent enters the compartment 212 through an inlet 221 located at its lower end.
- the treated effluent leaves through an outlet 224 located at the upper end of the compartment 212.
- a recycling circuit 230 is further provided between a second outlet 231 also located on the side of the upper end of the compartment 212 and a second inlet 232 located upstream of the current collector, in other words upstream of the first stage E1 with respect to the circulation of the effluent inside the compartment, here according to an ascending current (see direction X in the figures).
- a circulation means 233 (pump, etc.) ensures the circulation of the treated effluent in the recycling circuit 230.
- FIG. 3 shows a microbial biofilm compartment equipped with another recycling system.
- the compartment 312 comprises a multi-stage current collector comprising here four stages E1 to E4 each defining a chamber intended to receive the support material (not shown). As seen in this figure, the section of each chamber extends over the entire surface of the internal section of compartment 312.
- the effluent enters the compartment 312 through an inlet 321 located at its lower end.
- the effluent thus also circulates in an upward current inside the compartment (see direction X in the figures).
- the treated effluent leaves through an outlet 324 located at the upper end of the compartment 312.
- a recycling circuit 330 connects a second outlet 331 also located on the side of the upper end of the compartment 312 and a second inlet 334 located between the first stage E1 and the second stage E2 of the current collector.
- a circulation means 333 (pump, etc.) ensures the circulation of the treated effluent in the recycling circuit 330.
- all or part of the effluent circulating inside the compartment 312 is recycled via the recycling circuit downstream of the first chamber of the current collector (chamber closest to the inlet of effluent to be treated), allowing the fluidization of the support material at the level of each of the stages located downstream, namely stages E2 to E4, while the support material of the first stage functions as a fixed bed.
- the recycle circuit 330 can also be connected to another input 332 located upstream of the first stage E1 so that according to the needs, recycling can allow the fluidization of the support material at all stages, as in the embodiment described with reference to Figure 2.
- the fluidization of the support material is obtained by the circulation of the effluent through the chambers of the current collector, this fluidization can also be promoted by injection of a fluidization gas.
- FIGS 4A, 4B, 5A, 5B schematically illustrate the possible circulations of fluids inside microbial biofilm compartments according to the invention according to different cases. These different circulation configurations can be implemented regardless of the layout of a microbial biofilm compartment as defined in the present invention.
- Each of these figures schematically represents a multi-stage current collector 415, 515, 615, 715 with two stages E1, E2, as well as the circulations of fluid through this current collector.
- Each stage has a chamber containing support material 17. As seen in these figures, the section of each chamber extends over the entire surface of the internal section of the microbial biofilm compartment.
- the case represented in FIG. 4A corresponds to a case without fluidization gas, in which the density of the support material 17 is greater than the density of the effluent.
- the effluent then circulates through the current collector 415 according to an ascending current between an inlet 421 of the compartment and an outlet 424.
- a recycling circuit 430 similar to that described with reference to FIG. 2 may or may not be provided.
- the case represented in FIG. 4B corresponds to a case with fluidization gas, in which the density of the support material 17 is greater than the apparent density of the effluent-fluidization gas mixture.
- the effluent then also circulates through the current collector 515 according to an ascending current between an inlet 521 of the compartment and an outlet 524, as does the fluidization gas which circulates between a lower inlet 541 and an upper outlet 542.
- a circuit recycling 530 similar to that described with reference to Figure 2 may or may not be provided.
- the case represented in FIG. 5A corresponds to a case without fluidization gas, in which the density of the support material 17 is lower than the density of the effluent.
- the effluent then circulates through the current collector 615 according to a downward current between an upper inlet 621 of the compartment and a lower outlet 624.
- a recycling circuit 630 may or may not be provided as shown.
- the case represented in FIG. 5B corresponds to a case with fluidization gas, in which the density of the support material 17 is lower than the apparent density of the effluent-fluidization gas mixture.
- the effluent then also circulates through the current collector 715 according to a descending current between an upper inlet 721 of the compartment and a lower outlet 724.
- the fluidization gas circulates according to an ascending current between a lower inlet 741 and an upper outlet 742.
- a recycling circuit 730 may or may not be provided.
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AU2022281134A AU2022281134A1 (en) | 2021-05-26 | 2022-05-20 | Optimised bio-electrochemical reactor, in particular for degradation of the chemical oxygen demand of an effluent |
EP22732290.6A EP4347508A1 (fr) | 2021-05-26 | 2022-05-20 | Reacteur bio-electrochimique optimise, notamment pour la degradation de la demande chimique en oxygene d'un effluent |
CN202280037129.2A CN117412928A (zh) | 2021-05-26 | 2022-05-20 | 优化的生物电化学反应器,特别是用于降解流出物的化学需氧量 |
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FR2105458 | 2021-05-26 | ||
FR2105458A FR3123347A1 (fr) | 2021-05-26 | 2021-05-26 | Reacteur bio-electrochimique optimise, notamment pour la degradation de la demande chimique en oxygene d’un effluent |
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US20130299400A1 (en) * | 2010-07-21 | 2013-11-14 | Cambrian Innovation Llc | Bio-electrochemical system for treating wastewater |
KR20180055508A (ko) * | 2016-11-17 | 2018-05-25 | 한국에너지기술연구원 | 막 전극 일체형 미생물 전기화학 시스템 및 이를 이용한 연수화 장치 |
WO2020053529A1 (fr) | 2018-09-13 | 2020-03-19 | Suez Groupe | Réacteur bio-électrochimique à double bio-anode, procédé de régénération anodique et utilisation du réacteur à l'électrosynthèse microbienne |
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2021
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- 2022-05-20 AU AU2022281134A patent/AU2022281134A1/en active Pending
- 2022-05-20 CN CN202280037129.2A patent/CN117412928A/zh active Pending
- 2022-05-20 WO PCT/FR2022/050969 patent/WO2022248797A1/fr active Application Filing
- 2022-05-20 EP EP22732290.6A patent/EP4347508A1/fr active Pending
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US20130299400A1 (en) * | 2010-07-21 | 2013-11-14 | Cambrian Innovation Llc | Bio-electrochemical system for treating wastewater |
KR20180055508A (ko) * | 2016-11-17 | 2018-05-25 | 한국에너지기술연구원 | 막 전극 일체형 미생물 전기화학 시스템 및 이를 이용한 연수화 장치 |
WO2020053529A1 (fr) | 2018-09-13 | 2020-03-19 | Suez Groupe | Réacteur bio-électrochimique à double bio-anode, procédé de régénération anodique et utilisation du réacteur à l'électrosynthèse microbienne |
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JIA, Y. H.J. H. RYUC. H. KIMW. K. LEET. V. T. TRANH. L. LEER. H. ZHANGD. H. AHN.: "Enhancing hydrogen production efficiency in microbial electrolysis cell with membrane electrode assembly cathode", JOURNAL OF INDUSTRIAL AND ENGINEERING CHEMISTRY, vol. 18, no. 2, 2012, pages 715 19 |
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CN117412928A (zh) | 2024-01-16 |
FR3123347A1 (fr) | 2022-12-02 |
EP4347508A1 (fr) | 2024-04-10 |
AU2022281134A1 (en) | 2023-11-23 |
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