WO2011038453A1 - Système bio-électrochimique - Google Patents

Système bio-électrochimique Download PDF

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Publication number
WO2011038453A1
WO2011038453A1 PCT/AU2010/001277 AU2010001277W WO2011038453A1 WO 2011038453 A1 WO2011038453 A1 WO 2011038453A1 AU 2010001277 W AU2010001277 W AU 2010001277W WO 2011038453 A1 WO2011038453 A1 WO 2011038453A1
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WO
WIPO (PCT)
Prior art keywords
anode
cathode
compartment
bioelectrochemical system
compartments
Prior art date
Application number
PCT/AU2010/001277
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English (en)
Inventor
Shelley Therese Brown
Rene Rozendal
Korneel Rabaey
Original Assignee
The University Of Queensland
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from AU2009904724A external-priority patent/AU2009904724A0/en
Application filed by The University Of Queensland filed Critical The University Of Queensland
Publication of WO2011038453A1 publication Critical patent/WO2011038453A1/fr

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    • 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
    • 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
    • H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
    • H01M8/241—Grouping of fuel cells, e.g. stacking of fuel cells with solid or matrix-supported electrolytes
    • 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
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells

Definitions

  • BIOELECTROCHEMICAL SYSTEM FIELD OF THE INVENTION The present invention relates to a bioelectrochemical system. BACKGROUND TO THE INVENTION
  • Bioelectrochemical systems typically comprise a housing or a vessel containing an anode compartment and a cathode compartment.
  • the anode compartment contains an anode and the cathode compartment contains a cathode.
  • One of the compartments typically the anode compartment, contains electrochemically active microorganisms that oxidise material (such as organic material and/or inorganic material) present in the anode compartment. This results in the transfer of electrons to the anode.
  • the anode is electrically connected or coupled to a counter electrode (cathode) at which a cathodic reaction takes place.
  • the cathodic reaction is a reduction reaction.
  • the cathode compartment may contain electrochemically active microorganisms.
  • the bioelectrochemical system may operate as a fuel cell (in which case electrical energy is produced) or as an electrolysis cell (in which case, electrical energy is fed to the bioelectrochemical system) (Rozendal, R. A., H. V. M. Hamelers, K. Rabaey, J. Keller, and C. J. N. Buisman. 2008. Towards practical implementation of bioelectrochemical wastewater treatment. Trends in Biotechnology 26:450-459).
  • the skilled person will understand that one or both of the anode compartment and the cathode compartment may contain electrochemically active microorganisms.
  • ions are typically allowed to flow between the anode and the cathode.
  • cations may pass from the anode compartment to the cathode compartment or anions may pass from the cathode compartment to the anode compartment (or both anions and cations may pass between the respective compartments).
  • An ion permeable membrane is typically used to ensure that the flow of ions takes place.
  • a liquid or solution is provided to the anode compartment and a liquid or solution is also provided to the cathode compartment.
  • Appropriate feeding arrangements and remove arrangements may be provided for feeding and removing the liquid or solutions to and from the anode compartments and the cathode compartments.
  • the solution being removed from the anode compartment (which has effectively being "treated” by passing through the anode compartment) may be subsequently fed to the cathode compartment.
  • different liquids and solutions may be fed to the anode compartment and the cathode compartment, respectively.
  • the present invention provides a bioelectrochemical system comprising:
  • each anode compartment is separated from a cathode compartment by an ion permeable membrane.
  • the bioelectrochemical system comprises a plurality of anode compartments and a plurality of cathode compartments, each anode compartment being adjacent to at least one cathode compartment.
  • the system comprises a plurality of anode compartments and at least one cathode compartment.
  • the at least one cathode compartment may include a plurality of cathodes.
  • the bioelectrochemical system may comprise a plurality of cathode compartments and at least one anode compartment.
  • the at least one cathode compartment may include a plurality of anodes.
  • the present invention provides a bioelectrochemical system comprising a plurality of anodes, and a plurality of cathodes, each anode being adjacent to at least one cathode, each anode being separated from an adjacent cathode by an ion permeable membrane, wherein the anodes are electrically connected to each other in parallel and the cathodes are electrically connected to each other in parallel.
  • the anodes will also be electrically connected to the cathodes in order to maintain an electrical circuit in the system.
  • the electrical circuit may comprise a conductor having very low resistance such that the conductor acts as an electrical short circuit between the anode and the cathode.
  • a power supply may be included in the electrical circuit.
  • a single ion permeable membrane is used to separate each anode electrode from an adjacent cathode electrode.
  • the single ion permeable membrane may be interwoven between the anode electrodes and the cathode electrodes.
  • Ion permeable membranes suitable for use in the present invention include any ion permeable membranes that may be used in bioelectrochemical systems (Kim et al., Environ. Sci. Technol., 2007, 41 , 1004-1009; Rozendal et al., Water Sci. Technol., 2008, 57, 1757-1762).
  • Such ion permeable membranes may include ion exchange membranes, such as cation exchange membranes and anion exchange membranes.
  • Porous membranes such as microfiltration membranes, ultrafiltration membranes, and nanofiltration membranes, may also be used in the bioelectrochemical system used in the present invention.
  • the ion permeable membrane facilitates the transport of positively and/or negatively charged ions through the membrane, which compensates for the flow of the negatively charged electrons from anode to cathode and thus maintains electroneutrality in the system.
  • a plurality of ion permeable membranes such as a plurality of separate ion permeable membranes, are used to separate the anodes from the cathodes.
  • each of the anodes or each of the cathodes are surrounded by an ion permeable membrane.
  • a plurality of ion permeable membranes may be provided in this regard.
  • the ion permeable membranes surrounding each of the anodes or each of the cathodes may comprise an ion permeable membrane in the form of a lamellae or an envelope.
  • the ion permeable membrane envelops an anode or a cathode.
  • a plurality of lamellae or envelopes of ion permeable membranes are formed and a plurality of electrode chambers are created by connecting the plurality of lamellae or envelopes at opposite ends.
  • the surface area of either the anode or the cathode places a limitation on the maximum rate of reaction or conversion taking place in that compartment.
  • the rate limitations occurring in the anode compartment also result in the same rate limitations occurring in the cathode compartment. Therefore, in some embodiments of the present invention, the anode has a larger surface area then the cathode.
  • the adverse outcomes arising from the surface area limiting effects taking place on the anode electrode can be minimised by virtue of the increased surface area of the anodes, when compared to the surface area of the cathodes .
  • the surface area of the anodes may be up to twice as large as the surface area of the cathodes.
  • one or more (or even each) anode compartment may be provided with two anodes and the cathode compartments may be provided with one cathode.
  • one or more anode compartments may be provided with an anode that has a larger surface area than the surface area of a cathode.
  • the present invention provides a bioelectrochemical system comprising one or more anodes and two or more cathodes or two or more anodes and one or more cathodes, wherein each anode is positioned adjacent to a cathode and each anode is separated from an adjacent cathode by an ion permeable membrane.
  • the number of anodes equals the number of cathodes.
  • a combination of multiple anodes and multiple cathodes is contained within one reactor unit, which can be connected to one or more similar reactor units in a serial electrical connection.
  • multiple reactor units can be assembled into a stack type configuration, as known to a person skilled in the art.
  • Figure 1 is a schematic side view of an arrangement of anode compartments and cathodes compartments in accordance with one embodiment of the present invention
  • Figure 2 is a schematic plan view of an arrangement of anode compartments and cathode compartments in accordance with another embodiment of the present invention
  • Figure 3 is a schematic plan view of an arrangement of anode compartments and cathode compartments in accordance with another embodiment of the present invention
  • Figure 4 is a schematic side view of an arrangement of anode compartments and cathode compartments in accordance with a further embodiment of the present invention
  • Figure 5 is a schematic side view of an arrangement of anode compartments and cathode compartments in accordance with another embodiment of the present invention
  • Figure 6 is a schematic side view of an arrangement of a compartments and cathode compartments in accordance with another embodiment of the present invention.
  • the cathodes are connected to each other in parallel and the anodes are connected to each other in parallel
  • Figure 7 shows a schematic top view of an apparatus in accordance with an embodiment of the present invention
  • Figure 8 shows a schematic side view of the apparatus shown in Figure 7;
  • Figure 9 shows a schematic overview of overall reactor connections and feed streams in accordance with an embodiment of the present invention.
  • Figure 10A and 10B show a graph of evolution of the current over time during the first (A) and second (B) test run on synthetic feed.
  • the current gradually exceeded 1 A in both cases, at which point the potentiostatic control became unstable.
  • the anode potential was lowered to -350 mV vs Ag/AgCl on day 39 for run 2;
  • Figure 1 1 shows a graph of evolution of current for a set anode potential of -200 mV versus Ag/AgCl using real wastewater.
  • a weekly pattern including a peak (on Mondays) can be observed. This Monday peak likely corresponds to higher pH and lower organics load at start up of the existing treatment plant. Overall, the baseline current gradually increased over the test period.
  • Figure 1 shows a schematic side view of an arrangement of anode compartments and cathode compartments suitable for use in a bioelectrochemical system in accordance with the one embodiment of the present invention.
  • the embodiment shown in figure 1 includes a first anode 10 positioned in a first anode compartment 12, a first cathode 14 positioned in a first cathode compartment 16, a second anode 18 positioned in a second anode compartment 20 and a second cathode 22 positioned in a second cathode compartment 24.
  • the electrodes 10, 14, 18, 22 may be positioned in a larger vessel (not shown).
  • Each of the electrodes 10, 14, 18, 22 have electrical connections 1 1, 15, 19, 21 extending therefrom. This allows the electrodes to be connected to the appropriate electrical circuits required to maintain electrical charge balance in each of the compartments.
  • each anode compartment is positioned such that it is adjacent to a cathode compartment.
  • the compartments are arranged such that a sequence of anode compartment, cathode compartment, anode compartment, cathode compartment, etc, is maintained. Therefore, each anode compartment is adjacent to a cathode compartment and each cathode compartment is adjacent to an anode compartment.
  • Each anode compartment is separated from an adjacent cathode compartment and by use of an appropriate ion permeable membrane. For example, anode compartment 12 is separated from cathode compartment 16 by membrane 17. Similarly, cathode compartment 16 is separated from anode compartment 20 by membrane 21.
  • anode compartment 20 is separated from cathode compartment 24 by membrane 25.
  • a further membrane 13 is shown positioned to the left of anode compartment 12. It will be appreciated that membrane 13 may be used to separate anode compartment 12 from an adjacent cathode compartment located to the left of anode compartment 12. Alternatively, the sequence of anode compartments and cathode compartments may end at the left-hand edge of anode compartment 12. In this case, membrane 13 will not be required and it can be replaced by the wall of the vessel that contains the compartments. In a similar fashion, if the sequence of anode compartments and cathode compartments continues to the right of cathode compartment 24, a further membrane will be provided to the right of cathode compartment 24. Alternatively, if the sequence ends at the right-hand edge of cathode compartment 24, a wall of the vessel that contains the compartments will be positioned to the right-hand side of cathode compartment 24.
  • a plurality of spaced, essentially parallel membranes are provided in order to separate the respective anode compartments from the adjacent cathode compartments and to separate the cathode compartments from the adjacent anode compartments.
  • the lower ends of the membranes are joined or sealed to the bottom of the vessel in order to prevent liquid transfer between the anode compartments and the cathode compartments.
  • FIG. 2 shows an alternative arrangement of anodes and cathodes suitable for use in a bioelectrochemical system in accordance with another embodiment of the present invention.
  • a plurality of anode electrodes 30, 32 are provided and a plurality of cathode electrodes 34, 36 are also provided.
  • Each anode is surrounded by an envelope or lamella formed from an ion permerable membrane.
  • anode 30 is surrounded by an envelope or lamella 31 formed from an ion selective membrane.
  • anode 32 is surrounded by an envelope or lamellar 35 formed from an ion permeable membrane.
  • anode 30 is positioned inside a anode compartment 33 that is defined in part by the envelope or lamella 31 of the ion permeable membrane.
  • anode 32 is positioned inside anode compartment 37 that is formed at least in part by envelope or lamella 35 of the ion permeable membrane.
  • the cathodes 34, 36 may be also positioned within separate cathode compartments or the cathodes 34, 36 may be positioned within a single larger cathode compartment.
  • Figure 3 shows an alternative arrangement of the ion permeable membrane for separating the anodes from the cathodes.
  • a single ion permeable membrane 40 is used to separate anode 41 from cathode 42, and to separate cathode 42 from anode 43, and to separate anode 43 from cathode 44.
  • the ion exchange membrane 40 is effectively interwoven between the adjacent anodes and cathodes to thereby separate the anodes from the adjacent cathodes.
  • Figure 4 shows a schematic side view of a further embodiment of the present invention.
  • the apparatus 50 includes an anode compartment 51, an adjacent cathode compartment 52, an anode compartment 53 and a cathode compartment 54. This sequence of anode compartment/cathode compartment may continue to the left of anode compartment 51 or to the right of cathode compartment 54.
  • the cathode compartment 52 is defined by an envelope or lamella of an ion permeable membrane 55.
  • the envelope or lamella of ion permeable membrane 55 may be formed by taking two separate ion permeable membranes, placing them on either side of the cathode and welding or otherwise joining their ends 56, 57 together.
  • cathode compartment 54 is formed from an envelope or lamella 58 of an ion permeable membrane.
  • Each cathode compartment contains a cathode.
  • cathode compartment 52 contains cathode 59.
  • Cathode compartment 54 contains cathode 60.
  • each anode compartment contains 2 anodes.
  • anode compartment 51 contains anodes 61 and 62.
  • anode compartment 53 contains anodes 63 and 64. Therefore, the apparatus 50 shown in figure 4 provides a bioelectrochemical system in which the surface area of the anodes is approximately double the surface area of the cathodes (by virtue of their being twice as many anodes as cathodes). Consequently, if the anode reactions are rate-limiting in the overall bioelectrochemical process, the overall throughput of the apparatus 50 can be increased by virtue of the increased surface area of anodes.
  • anodes will be in electrical connection with the cathodes in order to complete an electrical circuit.
  • appropriate feed and effluent arrangements can be made to ensure that appropriate fluids or solutions are fed to and removed from the anode compartments and the cathode compartments.
  • FIG. 5 shows a schematic side view of an apparatus in accordance with another embodiment of the present invention.
  • the arrangement of anode compartments and cathode compartments shown in figure 5 is generally similar to that shown in figure 4 and, for convenience, like features are denoted by like reference numerals.
  • anode compartment 51 is provided with two anodes 61, 62.
  • Adjacent cathode compartment 52 is provided with cathode 59.
  • Anode compartment 53 is provided with two anodes 63, 64.
  • Cathode compartment 54 is provided with cathode 60. Additional anode compartments and cathode compartments are also included in the embodiment shown in figure 5.
  • the cathode compartments are defined, at least in part, by a lamella or envelope of ion permeable membrane, such as shown by reference numerals 55 and 58.
  • the anode compartments and cathode compartments are contained within a larger vessel 70.
  • the vessel 70 includes an inlet 71 through which a feed solution is fed to the vessel.
  • the anode compartments are open to the feed solution and therefore the feed solution flows into a bottom sump region (denoted by reference numeral 72) and then flows upwardly (as shown by arrows 73) through the anode compartments.
  • the solution leaving the anode compartments flows upwardly and out of the vessel 70 (as shown by arrows 74). Therefore, a simple feed arrangement for feeding solution to the anode compartments is provided, which feed arrangement has only a single inlet 71 to the vessel 70. As there is only a single inlet 71 to the vessel 70, the risk of clogging of the inlet is minimised.
  • the position and number of inlets can be varied according to the requirements and situation in which the bioelectrochemical system is deployed. Further, effluent solution leaving the anode compartments may simply overflow from the vessel 70 for subsequent collection. Alternatively, the vessel 70 may be provided with a liquid outlet through which the effluent solution passes. In certain embodiments, the bottom sump may contain structures to enable solids separation prior to entry of the aqueous solution in the bioelectrochemical system.
  • Appropriate electrochemical solutions may be fed to the cathode compartments by use of a manifold arrangement that passes the solution to the cathode compartments. This arrangement is not shown in figure 5.
  • the envelopes or lamellae of the ion permeable membranes may have open regions or ends that are placed in fluid communication with fluid inlets and fluid outlets to respectively supply and withdraw electrochemical solutions from the cathode compartments.
  • Figure 6 shows another arrangement of anodes and cathodes suitable for use in the present invention.
  • the arrangement shown in figure 6 is generally similar to that shown in figure 1 and, for convenience, like reference numerals are used to denote like parts. These features need not be described further.
  • the respective anodes 10, 18, etc are electrically connected to each other in parallel, using an anode current collection line 80 with appropriate respective anode electrical lines 11, 19 extending to the respective anodes 10, 18 or current collectors connecting to the respective anodes 10,18.
  • the respective cathodes 14, 22 are electrically connected to each other in parallel, for example, using a cathode current supply line 82 that has respective cathode electrical lines 15, 21 extending to the respective cathodes 14, 22.
  • FIG. 7 and 8 provides a schematic overview of a reactor 100 in accordance with another embodiment of the present invention.
  • Figure 7 shows a top view whilst figure 8 shows a side view of the reactor 100.
  • a lamellar type reactor was constructed by creating 2 welded cation exchange membrane (CMI-7000, Membranes International Inc.) envelopes 101 of 1 cm thickness.
  • the reactor matrix 100 has a bottom sump 120 and a top sump 122 that are in fluid communication with the anode chambers.
  • Anode feed solution is fed via feed line 124.
  • Anode effluent is removed via effluent line 126.
  • a pressure vent 128 is provided in the anode and forward line 126 to facilitate venting of any excessive gases that may be generated by the anode reactions.
  • Anode feed line 124 is fed with various feed materials, which may include the bulk feed 130 and concentrated feed 132.
  • the anode effluent is partly sent to disposal via line 134 and partly recycled to the anode feed line 124 via recycled line 136.
  • cathode compartments are fed with cathode feed solution via cathode feed line 140.
  • Fluid from the cathode chambers are removed by cathode effluent line 142.
  • the cathode effluent may be fed to a buffer vessel 144 that can be used to store cathode effluent.
  • the cathode effluent may be partly sent to disposal via disposal 146 and partly recycled to the cathode feed line 140 via recycle line 148.
  • Appropriate valves 150, 152, 154 and 156 are provided to control flow of the various streams.
  • a bioelectrochemical system was constructed in accordance with the embodiment shown in figures 7 to 9.
  • the total anode liquid volume was 1.02L
  • the total cathode volume was 0.61L. These volumes do not include the sumps and a small space next to the cathodes, including wall thickness the total reactor volume was ultimately 3.313L.
  • the inoculum for the initial start up of the reactor was obtained from a lab scale microbial fuel cell, fed with wastewater from the mixing tank of a brewery wastewater treatment plant as well as from a pilot scale microbial fuel cell fed with brewery wastewater.
  • the anode was fed with a mixture of two media.
  • the basic medium (initially 6.9 L d "1 , increased up to 30 L d "1 ) contained per liter: 0.1 g NH 4 CI, 0.1 g KH 2 P0 4 , 0.1 g MgS0 4 .7H 2 0, 0.02 g CaCl 2 .2H 2 0 and 1 ml of nutrient solution as described in Rabaey, K.; Ossieur, W.; Verhaege, M; Verstraete, W., Continuous microbial fuel cells convert carbohydrates to electricity. Wat Sci. Technol. 2005, 52, (1-2), 515-523.
  • a concentrate containing sodium acetate (as appropriate for increasing current, starting at 3.93 g acetate L “1 ) and NaHC0 3 (variable quantity to ensure pH neutrality of the incoming concentrate) was added as required to achieve a target current density depending on the status of the reactor.
  • the flow of this concentrate was varied to achieve increasing loading rates (starting rate was 0.7 L d "1 ),
  • the operational period can be divided in three runs: (i) first lab based run (ii) second lab based run and (iii) brewery based run.
  • the cathode only contained the corrugated mesh as cathode and current collector.
  • the system was operated for 64 days, during which the anode feed was progressively increased by increasing both concentrate concentration and flow. The experiment was terminated shortly after a failure due to gas production. Imperfect sealing between anode and cathode was observed, therefore the reactor was dismantled and rebuilt.
  • the finer meshes were inserted into the cathodes to serve as electrode, next to the corrugated mesh as current collector. The system was then operated for 46 days.
  • the reactor was moved to a brewery where "mixing tank” wastewater was fed to the reactor.
  • the composition of the incoming wastewater can be seen in Table 1.
  • the influent was mixed in (1/1) with anaerobic digester effluent to achieve a higher influent pH and gain more alkalinity (composition also in Table 1).
  • the cathode flow was 0.71 L d "1
  • the anode influent flow was varied between 51 and 702 L d "1 .
  • the reactor was further operated using a pump both for the cathode influent and effluent at equal flow rates to prevent crossover of anode fluid to the cathode.
  • the current increased to 1.015 A on day 62.
  • the applied voltage over the BES was 1.77 V, which gives a calculated cathode potential of -2.07 V vs Ag/AgCl.
  • this value is off by the ohmic resistance of the system and the pH related potential difference. Impedance spectroscopy was performed, giving an estimated ohmic resistance of 0.14 ⁇ . Expressed as a volumetric resistance (considering 1.63 L volume in total) this implies that the resistance was 0.23 ⁇ m 3 .
  • the pH of the anode effluent remained quite constant at 7.00 ⁇ 0.35. Based on the influent and effluent concentrations, the acetate removal was 61 ⁇ 20% over the experimental period.
  • the pH of the cathode liquid gradually increased (average 12.5 ⁇ 1.6 after the lag phase) reaching a value of 13.93 on day 42. This corresponds to a 3.4 %WT concentration of hydroxyl expressed as NaOH.
  • the average current generated was 0.710 ⁇ 0.100 A, which leads to an efficiency of current to caustic conversion of 96%.
  • the coulombic efficiency for acetate oxidation was 63%) (removal 75%), leading to overall acetate to caustic coulombic efficiency of 61%.
  • Table 1 shows typical ananysis for the mixing tank effluent and the anaerobic digester effluent.
  • alkalinity is generated and thus a mix-in of digester effluent will improve the buffering capacity of the BES influent.
  • This modification did not completely alleviate the weekly fluctuations, however it was maintained throughout the experimental period.
  • the slow increase of the current indicates that the microbial community had to adapt considerably to the change in feed conditions.
  • the baseline current consistently increased, with the weekly peak reaching a value of 0.38 A.
  • Table 2 summarizes the analytical data over time for the influent and effluent of the anode and the cathode.
  • the caustic strength was low for this experimental period: while theoretically the pH could go up to 13.4 for an assumed average current density of 0.2A on a daily basis, 12.54 was the maximal measured value.
  • the increased conductivity over time confirms the transport of cations from anode to cathode.
  • Table 1 Representative composition of the mixing tank wastewater and anaerobic digester effluent obtained at the brewery. All concentration values are given in mg L "1 .
  • Embodiments of the present invention provide a number of benefits when compared with previous bioelectrochemical systems.
  • the present invention allows for the provision of bioelectrochemical system units that can be used with other bioelectrochemical system units in a modular manner. This allows for easy scale up by simply adding further modules to the overall system.
  • Some embodiments of the present invention also allow for parallel current collection/connection between multiple anodes and parallel current collection/connection between multiple cathodes. This simplifies both manufacture and operation of the system.
  • sumps or manifolds may be used to feed and/or remove liquid or solution from the respective anodes and cathodes. Again, this simplifies construction and operation.
  • the risk of clogging of the liquid inlet and outlet can be decreased, for example, by having one common inlet for a multitude of anodes or cathodes, as described previously.
  • improved conversion or rate of reaction can be obtained by increasing the surface area of the electrodes in the limiting electrode reaction compartments.
  • this will be the anode reaction and in these embodiments the surface area of the anodes can be increased relative to the surface area of the cathodes, for example, up to twice the anode surface area compared to the cathode surface area.

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  • Engineering & Computer Science (AREA)
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Abstract

L'invention concerne un système bio-électrochimique comprenant au moins un compartiment sélectionné à partir d'un compartiment d'anode ou d'un compartiment de cathode et deux ou plusieurs autres compartiments sélectionnés à partir de l'autre compartiment parmi le compartiment d'anode et le compartiment de cathode. Chaque compartiment d'anode est séparé du compartiment de cathode par une membrane perméable aux ions.
PCT/AU2010/001277 2009-09-29 2010-09-29 Système bio-électrochimique WO2011038453A1 (fr)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013049940A1 (fr) * 2011-10-04 2013-04-11 Valorbec S.E.C. Micro-cellules d'alimentation extensibles ne présentant pas d'espace entre les éléments de transfert d'électrons et de protons
IT202000010324A1 (it) * 2020-05-08 2021-11-08 Samuele Falciani Cella a combustibile microbica

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Publication number Priority date Publication date Assignee Title
US20060147763A1 (en) * 2004-12-30 2006-07-06 Angenent Largus T Upflow microbial fuel cell (UMFC)
US20070259217A1 (en) * 2006-05-02 2007-11-08 The Penn State Research Foundation Materials and configurations for scalable microbial fuel cells
WO2008059331A2 (fr) * 2006-10-03 2008-05-22 Power Knowledge Limited Réacteur bioélectrochimique
WO2008110176A1 (fr) * 2007-03-12 2008-09-18 Danmarks Tekniske Universitet (Technical University Of Denmark) Cellule électrochimique microbienne
US20090017512A1 (en) * 2006-12-06 2009-01-15 May Harold D Apparatus and methods for the production of ethanol, hydrogen and electricity

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060147763A1 (en) * 2004-12-30 2006-07-06 Angenent Largus T Upflow microbial fuel cell (UMFC)
US20070259217A1 (en) * 2006-05-02 2007-11-08 The Penn State Research Foundation Materials and configurations for scalable microbial fuel cells
WO2008059331A2 (fr) * 2006-10-03 2008-05-22 Power Knowledge Limited Réacteur bioélectrochimique
US20090017512A1 (en) * 2006-12-06 2009-01-15 May Harold D Apparatus and methods for the production of ethanol, hydrogen and electricity
WO2008110176A1 (fr) * 2007-03-12 2008-09-18 Danmarks Tekniske Universitet (Technical University Of Denmark) Cellule électrochimique microbienne

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2013049940A1 (fr) * 2011-10-04 2013-04-11 Valorbec S.E.C. Micro-cellules d'alimentation extensibles ne présentant pas d'espace entre les éléments de transfert d'électrons et de protons
US10615440B2 (en) 2011-10-04 2020-04-07 Muthukumaran Packirisamy Scalable micro power cells with no-gap arrangement between electron and proton transfer elements
IT202000010324A1 (it) * 2020-05-08 2021-11-08 Samuele Falciani Cella a combustibile microbica
WO2021224951A1 (fr) * 2020-05-08 2021-11-11 RINDI, Tommaso Pile à combustible microbienne

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