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WO2003016461A2 - Systeme de bioreacteur permettant l'utilisation du degagement de chaleur de reactions biochimiques - Google Patents

Systeme de bioreacteur permettant l'utilisation du degagement de chaleur de reactions biochimiques Download PDF

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Publication number
WO2003016461A2
WO2003016461A2 PCT/EP2002/009246 EP0209246W WO03016461A2 WO 2003016461 A2 WO2003016461 A2 WO 2003016461A2 EP 0209246 W EP0209246 W EP 0209246W WO 03016461 A2 WO03016461 A2 WO 03016461A2
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WIPO (PCT)
Prior art keywords
bioreactor
iii
aerobic
essentially
heat
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/EP2002/009246
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German (de)
English (en)
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WO2003016461A3 (fr
Inventor
Udo Hölker
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hofer Bioreact GmbH
Original Assignee
Hofer Bioreact GmbH
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 DE10139348A external-priority patent/DE10139348A1/de
Priority claimed from EP01120067A external-priority patent/EP1285959A1/fr
Application filed by Hofer Bioreact GmbH filed Critical Hofer Bioreact GmbH
Priority to EP02794799A priority Critical patent/EP1421171A2/fr
Publication of WO2003016461A2 publication Critical patent/WO2003016461A2/fr
Publication of WO2003016461A3 publication Critical patent/WO2003016461A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/58—Reaction vessels connected in series or in parallel
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/18—External loop; Means for reintroduction of fermented biomass or liquid percolate
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • C12M41/12—Means for regulation, monitoring, measurement or control, e.g. flow regulation of temperature
    • C12M41/18—Heat exchange systems, e.g. heat jackets or outer envelopes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present invention relates to a bioreactor system for utilizing the microbial heat development in the metabolism of organic substrates and a continuous process for the microbial degradation of organic substrates in order to obtain thermal energy.
  • the metabolism of organic substrates by microorganisms takes place through successive oxidation of the substrate used up to CO 2 .
  • the substrate is used to store chemical energy in the form of ATP and to build up the cell mass. With each chemical reaction, part of the internal energy (H) is lost as entropy S (heat).
  • H internal energy
  • entropy S heat
  • FR 2466502 describes a method in which several aerobic and anaerobic steps are carried out with the aid of a pre-fermenter and three anaerobic fermenters.
  • the pre-fermenter is thermally insulated and contains a heat exchanger that is connected to a boiler that is also operated with the help of part of the biogas produced.
  • manure is preheated to facilitate aerobic fermentation.
  • the substrates are mixed by a stirring device, a circulation pump and a feed of the fermentation material.
  • the fermentation material is fed from one to the next fermenter from below at the base of the fermenter.
  • the reaction is carried out by stirring systems and pumps, which remove the substrates from the top of the reactor, pass them through an external heat exchanger and feed them back to the bottom of the reactor.
  • the device described in FR 2466502 is used for the production of biogas.
  • DE-A-4427644 describes a process for the treatment of bio-residues.
  • the rotting and removal of the residues takes place in one (or several parallel) mixing reactors. Parts of the residues treated in this way are then further broken down in a downstream anaerobic reactor stage.
  • DE-A-19946299 and DE-C-4115435 describe multi-stage, aerobic-anaerobic processes for the treatment of residues, in the first case organic residues e.g. B. from household waste, whereby methane is formed, which is burned, in the second case explosive residues for the purpose of disposal. Both processes use the waste heat released during or at the end of the process to heat other intermediate process stages. External use of the waste heat outside of the overall process is not possible with these processes.
  • DE-C-4227238 describes a method for operating sewage treatment plants, in which the through biodegradation processes released heat is partly used for heating domestic water or heating water outside the process.
  • this process is not a closed, regulated system with bioreactors with the aim of optimally generating externally usable thermal energy.
  • the object of the invention was to provide central or decentralized bioreactors that can be installed in every household.
  • the aim is to produce the greatest possible constant heat at the highest possible temperature, to dissipate this via a heat exchanger and to use it for hot water production and electricity generation.
  • the thermal fermentation should be carried out with high solids contents in order to be able to utilize organic household waste and to use as little water as possible.
  • the invention thus relates
  • a bioreactor system for utilizing the heat development of biochemical reactions, in particular for hot water and electricity production, with a bioreactor (1, 11) for essentially aerobic microbial degradation of organic substrates, a bioreactor (III) for essentially anaerobic microbial degradation of organic substrates, wherein the bioreactors (1, 11, 111) are connected in succession so that the degradation substrate of the upstream bioreactor (I) or (II) is fed to the downstream bioreactors (II, III), and at least one heat exchanger for removing heat from the bioreactors (1, 11, 111);
  • bioreactor system for utilizing the heat development of biochemical reactions, in particular for hot water and electricity production, with two bioreactors (1, 11) for essentially aerobic microbial degradation of organic substrates, the bioreactors (1, 11) being connected in succession so that the degradation substrate of the upstream bioreactor (I) is fed to the downstream bioreactor (II), and at least one heat exchanger for dissipating heat from the bioreactors (1, 11);
  • a heat exchanger is provided to use the heat.
  • the heat exchanger can be coupled to the individual bioreactors.
  • the provision of a single heat exchanger or a common heat exchanger for two or more bioreactors has the consequence that the temperatures of these bioreactors are coupled to one another.
  • a particular advantage of the bioreactor system according to the invention is that it is preferably possible to use heat directly for hot water preparation and / or for heating purposes, without an intermediate production of biogas.
  • biogas is generated in an anaerobic bioreactor, this is preferably used to generate electricity, which then mainly or exclusively serves to energize the entire process itself, for example for operating pumps and the like.
  • the preferred regulation according to the invention of one or both aerobic bioreactors via the supply of air or oxygen is particularly important.
  • Another important aspect of the invention is the preferred routing of exhaust air from the first aerobic bioreactor into the second aerobic bioreactor. Such recirculation of the exhaust air increases the efficiency of the bioreactor system.
  • the bioreactor system according to the invention is particularly suitable for fermentation at high solids contents (from 110-70% by weight).
  • two essentially aerobic bioreactors and one essentially anaerobic bioreactor are provided.
  • the three bioreactors are connected one after the other, the first being the two aerobically operating bioreactors and then the anaerobically operating bioreactor.
  • the first bioreactor is preferably a solid bioreactor, to which oxygen is preferably supplied through a nozzle arrangement.
  • the second bioreactor is preferably a fluidized bed bioreactor in which the organic substrates are kept in solution due to the media flow.
  • the medium continuously conveyed in the second bioreactor preferably by removal in the upper region and supply in the lower region, is preferably passed through a ventilation and regulating device. In this, the medium is preferably enriched with oxygen and the pH is regulated.
  • the exhaust gases or the exhaust air from the first bioreactor for this purpose.
  • can from the ventilation and Regulator also exhaust gases are discharged. Since these are generally combustible gases, they are preferably fed to a combustion device.
  • the combustion device can in turn be used for energy generation, in particular for hot water preparation or electricity generation.
  • the first aerobic bioreactor and the anaerobic bioreactor are preferably equipped with a plurality of grid-like sieves, so that a gradual differentiation into fractions of different particle sizes takes place within the reactors. This is advantageous compared to a fractionation between reactors connected in series, since this enables particle transport according to the degree of degradation within a reactor body.
  • the exhaust air from the second aerobic reactor and / or the third anaerobic reactor is preferably fed to a burner, if appropriate after passing through a heat exchanger, in order to minimize the emissions. Since the exhaust air from the first aerobic bioreactor can still contain relatively large concentrations of oxygen, this exhaust air is preferably fed in a ventilation and regulating device to the second aerobic bioreactor in countercurrent.
  • the figure shows a bioreactor system with three bioreactors, the first two bioreactors (I and II) being used essentially for aerobic microbial degradation of organic substrates and the bioreactor (III) serving essentially for anaerobic microbial degradation of organic substrates.
  • the bioreactors (I, II, III) are connected in series.
  • This embodiment represents a preferred solution of both of the bioreactor systems described above, with the bioreactor (I or II) can be dispensed with, so that an essentially aerobically operating bioreactor precedes an essentially anaerobically operating bioreactor (III).
  • the bioreactor (III) in which essentially anaerobic microbial decomposition of organic substances takes place, can be omitted, so that only two aerobic bioreactors connected in series are provided.
  • a schematic diagram of a first preferred embodiment of the bioreactor system is shown in FIG. 1 .
  • An upstream first bioreactor (I) can have high solids contents, e.g. organic wastes, which do not have to be processed in addition, are operated and are preferably suitable for mushrooms.
  • the fermentation rate and thus the constant heat development in the bioreactor is guaranteed by the targeted supply of the microorganisms with oxygen.
  • the proposed bioreactor allows the continuous use of the heat released during the breathing of organic materials by microorganisms.
  • the first bioreactor I which is an essentially aerobically operating bioreactor, has a reaction container 12 closed with a lid 10. By opening the lid 10 and, for example, by mechanically moving the lid 10 in the direction of the arrow 14, organic substrates with a high solids content can be fed into the reaction container 12.
  • a comminution device for comminuting the organic waste can also be provided, which or the like via a pipe. is connected to an opening of the reaction container 12 in order to feed the substrates.
  • the first bioreactor I has a nozzle arrangement 16 with a plurality of vertically running nozzles 18. Oxygen can be supplied to the container 12 through the nozzles 18, which are preferably distributed regularly over the entire container 12.
  • the nozzle arrangement 16 is preferably connected to a compressor.
  • the individual nozzles 18 of the nozzle arrangement 16 can end at different heights of the container 12. They preferably extend through the entire container, so that the lower nozzle openings 20 are arranged in the lower region of the container 12.
  • Each individual nozzle 18 can have a plurality of air outlet openings, which are distributed over the height of the container 12. Through the nozzle arrangement, the substrates in the container 12 are aerated and mixed.
  • a plurality of preferably horizontally arranged screens 22 are provided within the container 12, the mesh size of the screens 22 preferably being reduced in the conveying direction.
  • the substrates in the first bioreactor I are conveyed in the vertical direction from top to bottom due to gravity.
  • the mesh size of the screens 22 thus decreases from top to bottom.
  • the nozzles 18 of the nozzle arrangement 16 preferably extend in the vertical direction and penetrate the sieves 22.
  • compressed air saturated with water is fed into the reaction container 12 through the nozzle arrangement.
  • the reaction rate of those in the container 12 can be adjusted Oxidation processes taking place and thus the amount of heat released during fermentation are controlled.
  • the reaction container 12 is double-walled, so that a suitable heat transport medium, such as water, can be provided in an intermediate space 26.
  • a suitable heat transport medium such as water
  • the double-walled container 12 is connected to a pipeline 28 in which a pump 30 is arranged.
  • the heat transport medium is removed from an upper region 32 of the container 12 and fed back to the lower region 24 of the container 12.
  • Heat is removed from the heat transport medium by means of a heat exchanger 34 arranged in the pipeline 28. This heat can be used to process hot water or to generate electricity.
  • a heat exchanger 34 arranged outside the reaction container 12
  • a heat exchanger provided inside the reaction container 12 can also be provided.
  • the substrates reaching the area 24 of the container 12 are transported to a second bioreactor II via a pipeline 38 via a conveying device 36, such as a screw screw.
  • a gas phase arises in the reaction container 12 during the fermentation of the organic substrates. This is discharged through a pipe 40.
  • the heat of the discharged gases can be used to preheat the air supplied through the nozzle arrangement 16 or to preheat the third anaerobic reactor, or it can be passed through a heat exchanger.
  • the gases discharged from the reaction vessel 12 of the first bioreactor I are at least partially used in the second bioreactor II (see below).
  • the substrate becomes in solution by a substrate stream flowing in the direction of the arrows 44 held.
  • medium is removed from an upper region of the container 42 and fed back to it via a pipe 46 by means of a pump 48 in a lower region of the container 42.
  • a further heat exchanger 48 is provided within the pipeline 46 for the direct removal of heat from the area.
  • the heat exchanger 48 can be coupled to the heat exchanger 34.
  • a ventilation and regulating device 50 is provided in the pipe output 46.
  • the ventilation and regulating device 50 serves to supply oxygen to the substrate and to regulate the pH.
  • Exhaust gases of the bioreactor I can be fed directly to the substrate processed in the bioreactor II via a feed line 52, which is preferably connected to the pipe 40 of the bioreactor I;
  • the gases supplied can be discharged via a second pipeline 54.
  • the gases discharged through the pipeline 54 are preferably fed to a combustion device 56.
  • the medium removed from the container 42 in the upper region is passed through a sieve and / or a filter 58.
  • the substrate present in the reaction container 42 is in turn heated by microbial oxidation processes.
  • the container 42 is preferably also double-walled, so that a heat transport medium, such as water, is transported through a cavity 60 and can absorb heat generated within the container 42.
  • the medium is transported via pipes 62 and a pump 64.
  • the medium is passed through a heat exchanger 66 to dissipate heat.
  • the heat exchanger 66 can be coupled to the heat exchanger 48 and / or the heat exchanger 34.
  • H 2 O is added to the sediment coming from the bioreactor I.
  • This "slurry" is further oxidized in a new aerobic process.
  • the temperature in the bioreactor should be kept constant. This is achieved by varying the admixture of oxygen in the aeration tank (50). Since the development of heat is primarily due to the use of O 2 as a terminal electron acceptor, the temperature and heat should also be regulated productively here by limiting or increasing the available oxygen.
  • the selected operating temperature in bioreactors I and II depends in both cases on the temperature tolerance of the microorganisms used.
  • a conveying device 68 is again provided, which can also be a screw screw.
  • the conveyor 68 conveys substrate through a pipeline 70 in the direction of the third bioreactor III.
  • the substrate is introduced into a reaction container 72 of the bioreactor III by means of a preferably vertical nozzle arrangement 74.
  • the nozzles preferably end at different heights in the reaction container 72.
  • the substrate is mixed in the reaction container 72, in which substrate in the upper region of the reaction container 72 is removed via a pipeline 76, conveyed by a pump 78 and via nozzles 80, preferably in lower region of the reaction container 72, this is fed back.
  • the reaction container 72 is preferably also double-walled, so that heat transport medium is provided in a cavity 82 and is conveyed via a pump 84 and pipes 86 through a heat exchanger 88 for the removal of heat.
  • the heat exchanger 88 can in turn be connected to the heat exchanger 34 and / or the heat exchanger 66 and / or the heat exchanger 68.
  • a further conveyor device 90 such as a screw screw, is provided in the lower region of the reaction container 72.
  • the remaining residual substrate which is essentially humus, is removed from the conveying device 90 through a pipeline 92.
  • the gases generated in the fermentation in the bioreactor III are discharged through a pipeline 94 and fed to the combustion device 56.
  • the mixing of the substrate in the reaction container 72 takes place either, as described above, through the nozzles 80 and the pump 78 or alternatively also through an agitator provided in the reaction container 72.
  • ARS I First aerobic stage
  • the novel bioreactor for the fermentation of solid substances enables the establishment of a system of controlled thermal use of organic residues.
  • a targeted ventilation, mixing and regulation was previously not possible in stirred bioreactors.
  • the first aerobic stage (ARS I) of this process is operated in continuous operation with a solids content of around 70%, i.e. without a macroscopically visible water phase.
  • Dry, moist or H 2 O-saturated compressed air which is provided by a compressor, enters the bioreactor through vertical nozzles 18, which can be inserted into the bioreactor, and aerates it evenly.
  • the nozzles are passed through sieves 22 (grids) with a decreasing exclusion volume.
  • the grids prevent the organic residues from pouring too hard, on the other hand they also serve for homogeneous ventilation (by distributing and breaking the possible air bubbles).
  • the grating system can be provided with openings to allow additional pulsed ventilation. Anaerobic regions in the fermentation material should be avoided in this fermentation stage in order to keep the methane content in the exhaust air low.
  • the warm exhaust air is discharged parallel to the supply air line to heat the supply air (energy conservation).
  • the exhaust air is passed on through the aerator in the second aerobic stage and from there into the methane burner after the anaerobic stage III in order to oxidize all VOCs (volatile organic carbon) formed during the fermentation.
  • the fermentation process can be influenced by adding water, possible growth substances or buffers (preferably acidic buffers that are suitable for fungi).
  • the temperature in the entire bioreactor system is to be regulated via the compressed air supply and thus via the availability of O 2 .
  • Exothermic reactions generally require O 2 , that is, the less O 2 is available to the aerobic microorganisms in the first two fermentation stages, the slower their metabolism and the less heat energy is released.
  • the lid 10 with the vertical nozzles can be raised completely or partially in order to refill organic residues and to clean the bioreactor if necessary.
  • the bioreactor is only started up in a small segment, otherwise anaerobic conditions can occur due to the interrupted ventilation and the undesired methane production in this stage can begin (emission protection).
  • the preferred embodiment for refilling organic residues is an antechamber which is closed off from the surroundings or the interior of the reactor by two flaps.
  • the outer flap When the outer flap is opened, the inner one is closed. After filling in the organic residues, the outer flap is closed, a shredder mechanism in the antechamber starts and crushes and homogenizes the residues. When this is done, the inner flap opens and the organic residues fall into the reactor. This procedure has the advantage that hardly any heat and no gases can escape from the reactor.
  • the entire reactor is well insulated and surrounded by a double jacket 26 filled with heat medium, which is connected to a heat exchanger 34.
  • a screw screw 36 is attached to the bottom of the reactor and continuously transports the sedimented sediment into the second aerobic bioreactor.
  • additional screw screws can be installed in the bioreactor at different heights, which ensure additional mixing.
  • Second aerobic stage (hereinafter also "ARS II"; preferably bacteria) Substrate is transported from (ARS I) via one or more screw screws. Before ARS II, the organic residue pre-oxidized and comminuted in ARS I is diluted with water to a solids content of 40% and added to reactor 12. This reactor is a closed system without a gas phase.
  • ARS II Second aerobic stage
  • the residue suspension is pumped in a circuit and kept in suspension by the continuous media stream 44.
  • the suspension is sieved and filtered, then passed through a heat exchanger 48 to generate energy.
  • a ventilation / measuring / control unit 50 Downstream of the heat exchanger is a ventilation / measuring / control unit 50, in which the O 2 concentration is measured and regulated by changing the compressed air supply in ARS I.
  • the air flow in ARS I increases, the O 2 content in its exhaust air increases, which is used again in the ARS II aerator.
  • additional compressed air is provided via the compressor preceded by ARS I.
  • the pH of the medium is regulated in the aerator (preferably neutral because of bacteria).
  • the solution is slightly alkalized and the HCO 3 formed during microbial breathing is complexed and precipitated by calcium.
  • the precipitated calcium carbonate is then regenerated in an acid scrubber, in which the bicarbonate is released as CO 2 .
  • the exhaust air from the aerator is passed through the methane burner of bioreactor III (ANRS III, see below) in order to burn the VOCs generated during fermentation.
  • a pump 49 feeds the medium enriched with oxygen back into the bioreactor at the bottom.
  • This bioreactor is also surrounded by a double jacket 60 which is filled with a heating medium and is coupled to a heat exchanger 66.
  • a worm screw 68 is attached to the bottom of the bioreactor and transfers sedimented residues into bioreactor III (ANRS III; see below).
  • ANRS III Third anaerobic stage
  • Substrate is transported from ARS II via one or more screw screws and diluted to a solids content of 10% by adding water.
  • the suspension is introduced through nozzles 78 projecting vertically into the reactor space (need not, but should be short).
  • the anaerobic reactor is mixed by a vertical nozzle system 80.
  • the suspension is pumped off at the top of the reactor and pressed in pulses through the nozzle system into the bioreactor.
  • the electricity generated in this way should be sufficient to energize all energy-consuming steps of the fermentation, such as shredders, pumps, heat pumps, screw screws and the compressor.
  • a screw screw 90 which transports the constituent not to be metabolized into waste containers.
  • the residue can be used as humus.
  • the method according to embodiment (3) of the invention comprises at least one essentially anaerobic and one essentially aerobic method step in discrete reaction vessels connected in series. It is preferred that at least one anaerobic process step is carried out first.
  • the process according to embodiment (4) of the invention comprises a continuous process for the microbial degradation of organic substrates for the production of thermal energy, comprising at least two essentially aerobic process steps in discrete reaction vessels connected in series.
  • the method according to embodiment (3) is used for the production of biogas, whereas that of embodiment (4) is suitable for the thermal use of the organic substrates.
  • the methods according to the invention comprise at least three fermentation steps, namely a first aerobic step (a), a second essentially aerobic step (b) and an essentially anaerobic step (c).
  • a first aerobic step (a) serving as supply air from step (b)
  • a second essentially aerobic step (b) serving as supply air from step (b)
  • an essentially anaerobic step (c) it is preferred that the process is operated as an essentially closed system, the exhaust air from step (a) serving as supply air from step (b), and the exhaust air from step (b) is burned together with the biogas generated in step (c).
  • the first two steps are controlled by the oxygen supply of step (a) (by using the exhaust air from step (a) as supply air from step (b), the oxygen supply of step (b) is also influenced thereby ).
  • (ii) is operated at a pH ⁇ 6, preferably a pH of 3 to 5, the degradation taking place essentially by fungi (e.g. mold, yeast, etc.); and or
  • citrate buffer
  • (i) is operated with a solids content of at least 25% by weight, preferably from 30 to 50% by weight; and or
  • (ii) is operated at a pH of> 7, preferably at a pH of 7 to 9, the degradation being carried out essentially by bacteria, in particular
  • Phosphate buffer and / or the addition of salts, in particular CaCl 2 , for
  • Step (c is an obligatory anaerobic fermentation reaction that
  • steps (a) - (c) the heat of reaction is removed by heat exchangers and / or that the exhaust air from step (c) is fed to an internal combustion engine.
  • - ARS I, ARS II, ANRS III are in a steady state when the system is in operation.
  • ARS I, ARS II and ARS III The daily turnover rates in ARS I, ARS II and ARS III correspond to 5, 10 and 20%.
  • ARS I a filling quantity of approx. 1100 kg (solids content 70%), this corresponds to a reaction volume of approx. 1500 I.
  • ARS II a filling quantity of approx. 400 kg (solids content 40%), this corresponds to a reaction volume of approx. 1000 I.
  • ANRS III a filling quantity of approx. 140 kg (solids content 10%), this corresponds to a reaction volume of approx. 1400 I.

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Abstract

La présente invention concerne un système de bioréacteur permettant l'utilisation du dégagement de chaleur d'origine microbienne résultant du métabolisme de substrats organiques, et un procédé permettant la dégradation microbienne continue de substrats organiques pour produire de l'énergie thermique.
PCT/EP2002/009246 2001-08-17 2002-08-19 Systeme de bioreacteur permettant l'utilisation du degagement de chaleur de reactions biochimiques Ceased WO2003016461A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP02794799A EP1421171A2 (fr) 2001-08-17 2002-08-19 Systeme de bioreacteur permettant l'utilisation du degagement de chaleur de reactions biochimiques

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE10139348A DE10139348A1 (de) 2001-08-17 2001-08-17 Bioreaktrosystem zur Nutzung der Wärmeentwicklung biochemischer Reaktionen
DE10139348.2 2001-08-17
EP01120067A EP1285959A1 (fr) 2001-08-21 2001-08-21 Bioréacteur pour l'utilisation de la chaleur dégagée par des réactions biochimiques
EP01120067.2 2001-08-21

Publications (2)

Publication Number Publication Date
WO2003016461A2 true WO2003016461A2 (fr) 2003-02-27
WO2003016461A3 WO2003016461A3 (fr) 2003-06-12

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EP (1) EP1421171A2 (fr)
WO (1) WO2003016461A2 (fr)

Cited By (2)

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EP2248886A3 (fr) * 2009-02-16 2013-09-25 Sang Bum Lee Digesteur anaérobique
EP3732282A4 (fr) * 2017-12-28 2021-10-13 Locus IP Company, LLC Réacteurs et méthodes de fermentation submergée pour production de produits à base de microbes

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CH655948A5 (fr) * 1983-11-09 1986-05-30 Armand Cotton Procede et installation de production de biogaz et de compost.
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2248886A3 (fr) * 2009-02-16 2013-09-25 Sang Bum Lee Digesteur anaérobique
EP3732282A4 (fr) * 2017-12-28 2021-10-13 Locus IP Company, LLC Réacteurs et méthodes de fermentation submergée pour production de produits à base de microbes
US12187999B2 (en) 2017-12-28 2025-01-07 Locus Solutions Ipco, Llc Reactors and submerged fermentation methods for producing microbe-based products

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