Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
  • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
  • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
  • B01F35/71—Feed mechanisms
  • B01F35/712—Feed mechanisms for feeding fluids
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
  • B01F27/60—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis
  • B01F27/70—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with paddles, blades or arms
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
  • B01F35/71—Feed mechanisms
  • B01F35/715—Feeding the components in several steps, e.g. successive steps
• • 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
  • C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
  • C12M27/02—Stirrer or mobile mixing elements
  • C12M27/06—Stirrer or mobile mixing elements with horizontal or inclined stirrer shaft or axis
• • 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
  • C12M41/22—Heat exchange systems, e.g. heat jackets or outer envelopes in contact with the bioreactor walls
• • C—CHEMISTRY; METALLURGY
  • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
  • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
  • C12M45/00—Means for pre-treatment of biological substances
  • C12M45/02—Means for pre-treatment of biological substances by mechanical forces; Stirring; Trituration; Comminuting
• • C—CHEMISTRY; METALLURGY
  • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
  • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
  • C12M45/00—Means for pre-treatment of biological substances
  • C12M45/04—Phase separators; Separation of non fermentable material; Fractionation
• • C—CHEMISTRY; METALLURGY
  • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
  • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
  • C12M45/00—Means for pre-treatment of biological substances
  • C12M45/20—Heating; Cooling
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F11/00—Treatment of sludge; Devices therefor
  • C02F11/02—Biological treatment
  • C02F11/04—Anaerobic treatment; Production of methane by such processes
• • 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
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
  • Y02W10/00—Technologies for wastewater treatment
  • Y02W10/20—Sludge processing
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
  • Y02W30/00—Technologies for solid waste management
  • Y02W30/40—Bio-organic fraction processing; Production of fertilisers from the organic fraction of waste or refuse

Definitions

• the invention relates to a method for the anaerobic fermentation of biogenic waste according to the preamble of claim 1 and a fermentation plant, in particular for performing such a method.
• MTT mechanical biological treatment
• the biogenic mass is broken down microbially, and a distinction can be made between aerobic and anaerobic microorganisms.
• the aerobic conversion ultimately leads to the end products carbon dioxide and water and is called rotting.
• the anaerobic conversion is typical for fermentation, the end products being methane, ammonia and hydrogen sulfide.
• DE 196 48 731 A1 describes an aerobic process in which the organic constituents of a waste fraction are washed out in a percolator and the residue is, for example, burned or deposited after drying.
• Percolation can take place, for example, in a box percolation plant according to WO 97/27158 AI.
• Experiments with a boiling-point heating system according to DE 101 42 906 AI, in which percolation is carried out in the boiling range of the process water, have also proved to be very promising.
• the organically highly contaminated outlet water drawn off from the percolator is fed to an anaerobic decomposition of a biogas plant, the organic part being converted by means of methane bacteria and being able to be fed to a biogas combustion for energy generation via a gas generation line.
• the above-described aerobic treatment of waste materials in a percolator has proven to be extremely competitive with the anaerobic processes and is becoming increasingly important.
• EP 0 192 900 B1 describes the so-called Valorga process - in which the fermentation takes place in a fermenter which is fed from below.
• the waste to be processed is carried in the form of a plug to a discharge which is arranged below the radially outer inlet opening.
• the waste is conveyed by injecting compressed biogas through gas nozzles arranged in several sectors of the fermenter, each sector being individually controllable in order to maintain the plug flow of the waste between the inlet opening and the discharge opening.
• EP 0 476 217 A1 discloses a heatable fermenter in which fresh material and digested material are fed to the fermenter as bacterial inoculum and the resulting digested material is transported to a digested material discharge via a stirrer. Such addition of inoculum can also be provided in the Valorga method described at the outset according to EP 0 192 900 B1.
• DE 196 24 268 AI discloses a fermentation process for waste in flowable form, ie with a dry matter content (TS) of less than 25%.
• a multi-chamber reactor is used, with the fermentation material being transported from an inlet opening through the chambers through to a discharge opening via an agitator.
• a common gas space is assigned to the multi-chamber reactor, from which the biogas generated during the fermentation process is drawn off.
• the metabolism in the individual chambers can be individually controlled by different process control, for example via heat exchangers, adding inoculum, etc.
• EP 0 794 247 A1 discloses a fermenter in which the digestate is introduced into a rotating drum in which a spiral is arranged.
• the digestate is guided in a plug-shaped manner from the inlet to the digestate discharge via this spiral. This promotion can be done by rotating the drum back and forth, with the forward rotation, i. H. the transport of the digestate in the direction of the digestate discharge takes longer than in the opposite direction, so that a predetermined dwell time of the digestate is achieved.
• the invention has for its object to provide a method for the anaerobic fermentation of biogenic waste and a fermentation plant with which the dwell time can be reduced significantly compared to conventional solutions.
• the anaerobic fermentation reactor (fermenter) is provided with a plurality of inlet openings and fermentation material discharge openings via which fresh material or fermentation material (the latter as inoculation material) can be supplied or fermentation material can be withdrawn.
• fresh material or fermentation material the latter as inoculation material
• fermentation material can be withdrawn.
• the metabolic process can be controlled so that the concentration of organic acids and ammonium within the fermentation reactor can be largely evened out.
• different concentrations occur in the different sections of the length of the reactor, which sensitively inhibit the fermentation process or even bring it to a standstill and thus considerably increase the residence time.
• the digestate is partially mixed and mixed Inoculation mass input along the flow path of the waste to be treated within the reactor - this means that the residence time can be reduced to a fraction of the residence times required in the prior art. It is to be expected that the residence time in the solution according to the invention is less than two days.
• the fermentation material is mixed within the fermentation reactor by means of a mechanical stirrer and / or by biogas injection, so that the fermentation process is further improved.
• the biogas is preferably pressed into the fermentation reactor via gas injection nozzles arranged in the reactor bottom.
• the gas injection nozzles are preferably combined in fields and controlled in succession.
• the gas injection is controlled in such a way that the floating blanket is broken open in the area of the respective controlled field.
• the interfering / heavy substances are conveyed to and removed from the middle of the fermentation reactor via two conveying devices.
• the fresh material / fermentation material is preferably fed and discharged via a central conveying station, via which the flow paths to and from the inlet / discharge openings can be reversed and thus correspondingly varying material flow profiles can be formed in the fermentation reactor.
• the formation of this material flow profile is supported by an agitator, whose direction of rotation can be reversed during the fermentation process.
• adjacent agitator blades of the agitator overlap in the axial direction, so that complete mixing of the reactor contents is ensured.
• the agitator can be made particularly simple if its agitator shaft is mounted on both sides in the reactor and the diameter is dimensioned such that the agitator shaft is adequately supported by the buoyancy generated in the reactor.
• the fermentation reactor is preferably arranged horizontally and has a round or approximately trapezoidal cross section. In the latter case, two inclined surfaces and a horizontal surface arranged between them are formed in the region of the reactor floor.
• the gas injection nozzles for injecting biogas are arranged in the area of the two inclined surfaces.
• the gas injection nozzles in the vertical direction i. H. open parallel to the vertical axis of the reactor or perpendicular to the inclined surfaces.
• the jacket of the fermenter can be heated to set an optimal operating temperature.
• a separate fresh material feed can also be provided be, via which fresh material can be fed regardless of the conveyor station.
• the fermentation plant according to the invention is particularly simple to assemble if the fermentation reactor is composed of transportable segments which are then assembled on site at the construction site.
• FIG. 1 shows a process diagram of the process according to the invention for the anaerobic fermentation of biogenic waste with a fermentation reactor according to the invention
• FIG. 2 shows a side view of the fermentation reactor from FIG. 1;
• FIG. 3 shows a side view of a further exemplary embodiment of a fermentation reactor and
• FIG. 4 shows a sectional top view of the fermentation reactor from FIG. 3;
• 5 shows the fermentation reactor from FIG. 3 in segment construction and
• FIG. 6 shows the fermentation reactor from FIG. 2 in segment construction and with a heavy material discharge system.
• FIG. 1 shows the process diagram of a process according to the invention for the anaerobic fermentation of biogenic waste.
• the fresh material 1 supplied contains, for example, domestic waste (residual waste) with a comparatively high organic content, organic waste from the separate collection, organically highly contaminated waste from the local ing industry and superimposed food, slaughterhouse waste, organically enriched food such as B. Active sludge from sewage treatment plants. Impurities 2 as well as impurities / heavy substances 4 occurring in the process steps described in more detail below are removed from this fresh material 1 and the remaining fresh material 1 is fed to a fermentation reactor 16. This produces fermentation gases as a metabolic product from the fermentation process, in particular biogas 3 (methane gas), which is drawn off overhead.
• biogas 3 methane gas
• digestate largely freed from the organic constituents is discharged after the fermentation process has ended and is subjected to further treatment such as dewatering, drying or composting. According to the legal regulations, digestate must be landfilled or incinerated from residual waste or at least processed into alternative fuels. Fermented material from organic waste or renewable raw materials can be used as a fertilizer or soil conditioner after dewatering and post-composting.
• the incoming fresh material is thus broken down into disruptive / heavy substances 2, 4, digestate 5 and biogas 3.
• the fresh material 1 supplied is first fed to a mechanical acceptance and processing system 8, which is sorted, comminuted and the contaminants 2 are discharged. Furthermore, this plant and preparation plant 8 unpacks superimposed foodstuffs and admixes and conditions additives and liquid waste, by means of which the dry matter content is adjusted.
• the processed and conditioned fresh material is then fed to a pump reservoir 9 and mixed there if necessary with dirty water 7, which Material cleaning according to FIG. 6 occurs, as will be described in more detail below.
• the storage container 9 is connected via a line 12 and slide 11 to a central pumping / delivery station 10, via which practically all the essential material flows of the system are controlled.
• the pumping / delivery station 10 can be operated both in the suction and in the pressure mode, so that either fresh material 1 is conveyed from the storage container 9 via lines 14 and suitably set sliders 11 to inlet openings 15 or fermentation material 5 via the lines 14 and correspondingly reversed slides 11 and disruptive / heavy goods can be withdrawn from the fermentation reactor 16 via a central discharge opening 16.3.
• the fermentation reactor 16 has an approximately cylindrical structure and is arranged horizontally, with a large number of inlet and discharge openings 15 and the central discharge opening 16.3 being provided along its outer diameter and its length.
• the inlet / discharge openings 15 can be used as an inlet opening for the fresh material or discharge opening for digestate.
• this suitable control can be used to set a desired material flow between the inlet / discharge openings 15, which is selected such that optimal mixing of the fermentation material is ensured.
• the pumping / delivery station 10 also makes it possible to draw off fermentation material, for example, via one of the inlet / discharge openings 15 and then to feed it in again as inoculation material via another of the inlet / discharge openings 15.
• the flow guidance is for example se so chosen that no significant differences in concentration of organic acids and ammonium occur within the reactor, so that the fermentation process can proceed in the predetermined manner.
• the pumping / conveying station 10 preferably uses rotary piston displacement or suction / pressure vessel systems as conveying members, which are used, for example, in agriculture or for sewer cleaning.
• the following functions can then in principle be carried out via the pump / delivery station 10: a) suction of fresh material 11 from the storage container 9 via the line 12; b) introduction of fresh material 1 from the template 9 into the reactor 16 via the inlet and outlet openings 15 or c) circulation of the reactor contents or fermentation sludge 20 at different points in the reactor 16 and in different directions via the inlet and outlet openings 15 and suitable slide positions 11 and through the lines 14.
• the cylindrical, lying fermentation reactor 16 shown in FIGS. 1 and 2 has an agitator 22 which is driven by two geared motors 22.1 which are supported on the end face of the reactor 16 and are torque-supported. These are controlled by frequency converters and can therefore be periodically reversed and / or depending on other operating parameters in their direction of rotation.
• agitator shaft 22.4 are evenly distributed on the circumference or lying in one plane Agitator arms 22.2 attached, which extend in the radial direction outwards to the peripheral wall of the fermentation reactor.
• axially parallel agitator blades 22.3 are fastened, the radial length of the agitator arms 22.2 being selected such that the agitator blades 22.3 slip over the digestate level 20.1 during rotation, so that a floating blanket that forms is destroyed or at least mixed.
• the axial length of the fermentation reactor 16 can easily be more than 30 meters. Since the aim of the invention is to provide as few internals as possible in the fermentation reactor 16, an agitator shaft 22.4 is dimensioned such that it is supported by the buoyancy of the fermentation sludge 20 in the fermentation reactor 16 and thus cannot sag - it can therefore be complicated to store within the Reactor room to be dispensed with.
• a gas space 3.1 is formed in the fermentation reactor 16, which opens into a gas dome 3.2 from which the biogas 3 is drawn off.
• two sediment discharge devices are provided, which in the embodiment shown in FIG. 1 are designed as two interacting moving floors 23. These convey the sediments in the axial direction to the centrally arranged discharge opening 16.3, through which the sediments (heavy / contaminants) can be discharged.
• the two moving floors 23 are each driven by a cylinder / piston unit 23.1 which can be actuated electrically or hydraulically. Via this cylinder / piston unit 23.1, the push floors 23 perform strokes in the direction of the arrows 23.2 in order to move the suspended matter in the direction of the discharge opening. to promote 16.3.
• the agitator blades 22.3 end somewhat above the push floors 23, so that the suspended matter is conveyed downwards by the agitator 22 within the reactor.
• the gas space 3.1 is secured by a safety device 33 so that no excess pressure can build up.
• the above-mentioned control of the geared motors 22.1 of the agitator 22 is designed such that by reversing the direction of rotation and suitable timing, the sediments 4 are evenly introduced into a discharge shaft of the moving floors 23 from both sides.
• a jacket 16.1 of the fermentation reactor 16 is provided with an insulation 16.1 in order to maintain a predetermined fermentation temperature.
• This fermentation temperature can be set by means of heating pockets 18 (FIG. 2), which are distributed on the outer circumference of the fermentation reactor 16 and can be controlled via the system control so that the predetermined temperature profile is set within the reactor.
• fresh material can also be supplied via a direct loading.
• This fresh material is branched off downstream of the storage container 9 via a correspondingly adjusted slide 11 and heated to the process temperature by means of a heat exchanger 17.
• the heat exchanger 17 is surrounded by a heating jacket 17.3 and has a guide tube 17.2 heated thereby, in which a conveying spiral 17.1 is arranged, via which the fresh material is drawn in and conveyed onward.
• the fresh material 1 heated to the process temperature is then over a further slide 11 and for example a spiral conveyor 32 conveyed into the interior of the reactor, the spiral conveyor 32 below the digestate level
• Preheated fresh material can be branched off downstream of the heat exchanger 17 via a further slide 11 and guided to the central pumping / delivery station 10 via a branch line 13.
• the discharge opening 16.3 can be formed by three or more parallel discharge regions 16.3a, 16.3b, 16.3c, via which the sediments conveyed by the push floors 23 are pushed towards the by means of slides 11a, 11b, 11c Delivery lines 14 can be discharged.
• FIG. 2 also shows very clearly that the agitator blades 22.3 scoop the sediments to the push floors 23 and, depending on the control of the slide 11 via the pumping / delivery station 10, 16 different digestate flow directions within the fermentation reactor
• the cylindrical reactor shape described above is comparatively easy to manufacture and is superior to other solutions in terms of compressive strength. Under certain conditions, however, it may also be necessary to design the fermentation reactor 16 with a different geometry. Such an embodiment is illustrated in Figures 3 and 4.
• the fermentation reactor 16 has an approximately rectangular cross section, the bottom being formed by two inclined surfaces 16.4 which are horizontal over one extending horizontal surface 16.5 are interconnected.
• the two sliding floors 23 and the discharge openings 16.3a, b, c are formed in the area of this horizontal surface 16.5.
• the inlet and discharge openings 15 are then located in the vertically extending side walls of the fermentation reactor 16.
• the material flows are controlled - as in the exemplary embodiment described above - via the central pump / delivery station 10, so that different material flow paths 20.2 can in turn be set within the fermentation reactor 1.
• a gas injection system is used instead of a mechanical agitator 22, i.e. a pneumatic agitator is used.
• the gas injection system has a plurality of nozzles 30.1, which preferably open into the inclined surfaces 16.4 of the fermentation reactor 16.
• nozzles 30.1 which preferably open into the inclined surfaces 16.4 of the fermentation reactor 16.
• two different nozzle mouth areas are shown.
• the nozzles 30.1 run approximately perpendicular to the inclined surface 16.4, while the nozzles 30.1 in the right part are arranged parallel to the vertical axis (vertical in FIG. 3) of the fermentation reactor 16. I.e. If the nozzles 30.1 are arranged as shown in FIG. 3 on the left, the injected gas flows obliquely to the vertical axis into the reactor space, while in the embodiment shown on the right it is pressed in parallel to the vertical axis.
• Biogas is used for the pneumatic conveying and circulation of the fermentation sludge 20
• Compressor 26 is sucked out of the gas dome 3.2 and then passed via a gas injection line 27 and a plurality of control valves 28, 29 and connected branch lines to a respective nozzle array 30, which each consists of a plurality of nozzles 30.1.
• the fields 30 are arranged one behind the other along the inclined surfaces 16.4 in the longitudinal direction of the reactor (perpendicular to the plane of the drawing in FIG. 3), each field 30 being able to be charged with biogas separately via the system control.
• the compressor 26 is arranged by the dimension H4 above the digestate level 20.1, so that when the compressor 26 is at a standstill no digestate 20 can enter the compressor via the gas injection line 27.
• the minimum gas pressure required to circulate the fermentation sludge 20 corresponds approximately to the barometric height (H2 x 1.5 (bar)) of the fill level that is required to overcome the pipeline resistance.
• the number of gas injection nozzles 30.1 per nozzle field 30 also depends on the dimensions x, y, that is, the length and width of the nozzle fields 30, 8 to 16 nozzles being arranged per m 2 of floor area depending on the height H2.
• the fields 30 are acted upon in succession with compressed gas in the longitudinal direction.
• the fermentation sludge 20 is displaced by the rising gas bubble and moved in the arrow direction according to FIG. 3 by the resulting suction, the nozzles 30.1 opening in the vertical direction initially ensuring an upward flow, while the obliquely opening nozzles 30.1 deflect the digestate flow to the right.
• the circulation can also take place opposite to the direction of the arrow.
• the exposure time via the nozzles 30.1 depends on the container height H2, H3 and the set solids content (TS).
• Each field 30 is gassed until an emerging floating cover 31.1 is torn open.
• the settling of the flow shown in FIG. 3 causes the sediments to settle on the inclined surfaces 16.4 and, due to the gradient, are conveyed to the two push floors 23, via which the sediments are conveyed to the centrally arranged discharge openings 16.3.
• the fermentation reactor 16 can be made with a considerable length (30 m). It is therefore not possible to transport the finished reactor vessel to the construction site. So far, this has to be manufactured on site, ie on the construction site, so that a considerable amount of production is required.
• the fermentation reactor 16 is produced from a large number of road-transportable elements, which are then assembled on the construction site with comparatively little effort.
• the container length L1 is divided into transportable elements with a length of approx. 12 to 15 m and a width bl of approx. 3 to 4 m.
• the overall height H1 corresponds approximately to a transport length of approximately 15 m with a width B1 (corresponds to the width of the inclined surfaces 16.4 and the horizontal surface 16.5 in the horizontal direction) of approx. 4 m.
• the container is subdivided into a large number of segments, each of which has a width b1 of 3 to 4 m and the aforementioned length of approximately 12 to 15 m, so that a comparatively simple transport to the construction site and quick assembly take place Location is enabled.
• FIG. 6 shows an example of a heavy material discharge device.
• the heavy materials deposited by the action of the mechanical agitator 22 or by the pneumatic conveyance via the nozzles 30.1 and conveyed from the push floors 23 to the centrally arranged discharge openings 16.3 first reach a discharge spiral conveyor 24 which enters an inclined conveyor 25.
• the heavy materials 4 are conveyed obliquely upwards to a washing installation 25.1, which is located above the digestate level 20.1.
• the contaminated heavy substances 4 are conveyed through a sieve basket which is charged with cleaning water 6 from the outside, through which the contaminants are rinsed out, so that cleaned heavy substances 4.1 are discharged.
• the contaminated cleaning water 7 is returned to the storage container 9 - (see FIGS. 1 and 2) and used there to adjust the TS content.
• the cleaned heavy materials 4.1 can be landfilled or used for other purposes. For example, process water or fresh water can be used as cleaning water 6.
• the digestate 5 obtained in the upcoming processes is a further treatment, for example one Dewatering, drying or composting.
• a mechanical stirrer can also be added to the gas inlet nozzles according to FIG. 3.
• the gas injection nozzles can also be used in a fermentation reactor with a round cross section according to FIG. 1.
• a process for the anaerobic fermentation of biogenic waste and a fermentation plant for carrying out this process are disclosed.
• the fresh material ie the biogenic waste to be treated
• the fresh material is fed in via a plurality of inlet openings distributed along the reactor height and / or reactor length and / or fermentation material is drawn off via a plurality of fermentation material discharge openings.

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• Chemical & Material Sciences (AREA)
• Health & Medical Sciences (AREA)
• Life Sciences & Earth Sciences (AREA)
• Engineering & Computer Science (AREA)
• Wood Science & Technology (AREA)
• Organic Chemistry (AREA)
• Bioinformatics & Cheminformatics (AREA)
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• Genetics & Genomics (AREA)
• General Engineering & Computer Science (AREA)
• Microbiology (AREA)
• Biotechnology (AREA)
• Biochemistry (AREA)
• Biomedical Technology (AREA)
• General Health & Medical Sciences (AREA)
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• General Chemical & Material Sciences (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Processing Of Solid Wastes (AREA)
• Treatment Of Sludge (AREA)
• Fertilizers (AREA)
• Apparatus Associated With Microorganisms And Enzymes (AREA)
• Preparation Of Compounds By Using Micro-Organisms (AREA)
• Mixers With Rotating Receptacles And Mixers With Vibration Mechanisms (AREA)

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• 2004
  • 2004-05-19 DE DE200410025318 patent/DE102004025318A1/de not_active Withdrawn
• 2005
  • 2005-05-19 CA CA 2567146 patent/CA2567146A1/en not_active Abandoned
  • 2005-05-19 WO PCT/EP2005/005452 patent/WO2005113469A1/de active Application Filing
  • 2005-05-19 EP EP05741235A patent/EP1756021A1/de not_active Withdrawn
  • 2005-05-19 RU RU2006141345/12A patent/RU2006141345A/ru not_active Application Discontinuation
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  • 2005-05-19 SG SG200718832-9A patent/SG138615A1/en unknown
  • 2005-05-19 US US11/596,811 patent/US20080032375A1/en not_active Abandoned
  • 2005-05-19 CN CNA2005800241064A patent/CN1989085A/zh active Pending
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  • 2006-11-17 ZA ZA200609566A patent/ZA200609566B/xx unknown
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  • 2006-11-19 IL IL179393A patent/IL179393A0/en unknown
  • 2006-12-15 NO NO20065839A patent/NO20065839L/no not_active Application Discontinuation

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