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WO2023027590A1 - Procédé de traitement de déchets organiques et de récupération de ressources - Google Patents

Procédé de traitement de déchets organiques et de récupération de ressources Download PDF

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Publication number
WO2023027590A1
WO2023027590A1 PCT/NO2022/050200 NO2022050200W WO2023027590A1 WO 2023027590 A1 WO2023027590 A1 WO 2023027590A1 NO 2022050200 W NO2022050200 W NO 2022050200W WO 2023027590 A1 WO2023027590 A1 WO 2023027590A1
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Prior art keywords
feedstock
fermenter
syngas
supply
thermo
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PCT/NO2022/050200
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English (en)
Inventor
Gang XIN
Steinar DANIELSEN
Carlos DINAMARCA
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Wai Environmental Solutions AS
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Wai Environmental Solutions AS
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Priority to CN202280057659.3A priority Critical patent/CN118139962A/zh
Priority to EP22861780.9A priority patent/EP4392536A1/fr
Publication of WO2023027590A1 publication Critical patent/WO2023027590A1/fr
Anticipated expiration legal-status Critical
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    • 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
    • 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
    • B09B3/60—Biochemical treatment, e.g. by using enzymes
    • B09B3/65—Anaerobic treatment
    • 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
    • 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
    • C12M43/00—Combinations of bioreactors or fermenters with other apparatus
    • C12M43/08—Bioreactors or fermenters combined with devices or plants for production of electricity
    • 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
    • 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
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/14—Drying
    • 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
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/20—Heating or cooling
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
    • C12P5/02—Preparation of hydrocarbons or halogenated hydrocarbons acyclic
    • C12P5/023—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B2101/00—Type of solid waste
    • B09B2101/70—Kitchen refuse; Food waste
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B2101/00—Type of solid waste
    • B09B2101/75—Plastic waste
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1269—Heating the gasifier by radiating device, e.g. radiant tubes
    • C10J2300/1276—Heating the gasifier by radiating device, e.g. radiant tubes by electricity, e.g. resistor heating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1681—Integration of gasification processes with another plant or parts within the plant with biological plants, e.g. involving bacteria, algae, fungi
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the present invention relates to a process for combined biological and thermo-chemical treatment of biological sludge, manure, food waste, slaughterhouse waste, lignocellulosic wastes and plastic-containing wastes to recovery energy, nutrients, and carbon storage material.
  • AD anaerobic digestion
  • lignocellulosic waste as woody feedstock, has an enormous potential for renewable energy production.
  • the global demand for biomethane was 23 TWh according to the International Energy Agent.
  • this type of biomass is currently not considered as primary raw material for AD plants, due to high pre-treatment costs and poor conversion rates for biomethane with state-of-the-art technologies.
  • the typical organic conversion rates in an AD are in the range of 40-50%, which means over 50% of the organic material passes through the AD and end up in the digestate.
  • Digestate is rich in nitrogen and phosphorus and can be used as organic fertilizer.
  • significant greenhouse gases (GHG) can still be produced and released from the digestate during storage, transportation, and application in the field 1 .
  • pollutants in the digestate such as microplastics and
  • thermophilic temperatures promote stronger inhibition of ammonium to methanogens, which in many cases leads to more unstable performance than mesophilic digesters, especially when treating high nitrogen content wastes such as sewage sludge, fishery sludge and chicken manure 4 .
  • Temperature-phased anaerobic digestion combines a thermophilic phase followed by a mesophilic phase, which is an approach to incorporate advantages of thermophilic digestion and mitigate the disadvantages through the addition of a mesophilic phase that enhances stabilization.
  • THP Thermal hydrolysis pre-treatment
  • the high temperature and high pressure required in the THP process demand high amounts of steam: typically, 0.8-1 .5 ton 12-bar steam required to pre-treat 1 ton sludge (dry matter).
  • lignocellulosic materials render them resistant to biodegradation.
  • a wide range of physical and chemical pretreatment methods of lignocellulosic materials have been studies to improve their biodegradability in AD.
  • the pretreatment methods includes milling, irradiation, liquid hot water (100-230 °C and 1 -28 bar), chemicals (alkali or acid), steam explosion (160-260 °C and 7-48 bar), wet oxidation (180-220 °C and 1 -12 bar) and biological pretreatment with fungi and enzymes .
  • various pretreatment techniques have been studied on numerous of lignocellulosic feedstocks, only a few of the reported techniques achieved high biogas yield with reasonable costs to be attractive.
  • organic feedstock can be refined to solids (char), pyrolysis liquid and gas (non-condensable gas).
  • the pyrolysis liquid can be separated into an oil phase (pyrolysis oil) and an aqueous phase (APL).
  • AD can convert aqueous pyrolysis liquid (APL) to biogas, but at high bio-oil dosages the AD was inhibited 6 .
  • the challenge is how to feed the majority of the syngas, including non-condensable gas, bio-oil and APL from pyrolysis to AD and still obtain high and stable biogas production.
  • DE102009020200A1 describes a method for operating a biogas plant where fermentation substrate (digestate) is first dried and then gasified, and syngas produced in the gasifier is scrubbed by the liquid fermentation substrate and the cleaned syngas is fed into a gas engine for electricity and heat production.
  • the fermenters are filled with methane producing microorganisms.
  • WO2018234058A1 describes a method for using a membrane to feed syngas into a digester and improve syngas mass transfer from gas phase to liquid phase in the digester for biogas production.
  • the syngas temperature must be below 55 °C, ideally at 35 °C.
  • the membrane is not designed to handle high temperature syngas.
  • the syngas pressure is not greater than 2.5 bar when it enters the membrane.
  • W02015003273A1 describes a method for converting organic feedstocks to syngas and biochar, and syngas is further separated into non-condensable gas and condensate and feed both non-condensable gas and condensate into digester for biogas production.
  • WO2017197508A1 describes a similar process and includes adding metal ions in digestate to form precipitate and then pyrolyze the digestate cake to enhance phosphorus recovery in biochar.
  • EP1754771 A2 describes a method for producing gas from a biomass gasification process and the gas is fed into a biomass fermentation process where biogas is produced. The gas after passing the fermentation process is used in a gas engine for electricity and heat production.
  • pyrolysis gas is recycled back to the anaerobic digester and the publication also indicates that a two-step anaerobic digestion process would be beneficial and the present of biochar in an AD process is also beneficial due to the water binding and metal adsorption capacity associated with biochar.
  • the biochar enhanced fermentation is also presented in another article (Title: Enhanced Ethanol Production from Syngas by Clostridium ragsdalei in Continuous Stirred Tank Reactor Using Medium with Poultry Litter Biochar, Applied Energy, Volume 236, 1269-1279, 2019).
  • a process for treatment of organic waste comprising the following step: i) supply a wet feedstock to a dryer and obtain a dried feedstock. ii) mix and pretreat the dried feedstock with a dry feedstock to obtain a mixed feedstock. iii) supply the mixed feedstock to a thermo-chemical process and produce a char fraction and a hot syngas. iv) discharge the char fraction and separate the hot syngas stream into warm syngas and tar in a tar separation unit.
  • the wet feedstock and the dry feedstock can be any solid organic streams chosen from the group consisting of garden waste, demolition wood, impregnated wood, plastic-containing waste, straw, sawdust, bark, white pellet, black pellet or combinations thereof.
  • the AD feedstock is preferably chosen from the group consisting of pre- treated food waste, biological sludge, manure, slaughterhouse waste or combinations thereof.
  • the headspace gas from the fermenter is supplied to the thermo-chemical process as carrier gas or is supplied to the second thermochemical process as fuel for production of hydrogen or heat.
  • the hydrogen or heat production in the second thermo-chemical process can be combined with supply of the biogas from the digester.
  • the biological reactions in the fermenter are preferably chosen from the group consisting of fermentation, hydrolysis, acidogenesis, fermentative hydrogen production, acetogenesis, homo-acetogenesis and combinations thereof.
  • reactions of methanogenesis are suppressed in the fermenter on purpose.
  • the biological reactions in the digester are preferably chosen from the group consisting of fermentation, hydrolysis, acidogenesis, fermentative hydrogen production, acetogenesis, homo-acetogenesis, methanogenesis and combinations thereof.
  • the method can comprise the additional steps of supplying the digestate from the digester to a dewatering unit and obtain a reject water fraction and a dewatered digestate fraction, and supplying the dewater digestate fraction to the dryer.
  • all or a part of the biogas from the digester is supplied to the second thermo-chemical process as additional fuel.
  • the thermo-chemical process comprises the following steps: a. supply the mixed feedstock and a headspace gas from the fermenter to a feed chamber and mix the feedstock and headspace gas; b. supply the mixture from the feed chamber to a thermo-mechanical unit and heat the mixture: c. obtain a char fraction and a hot syngas; d. supply the hot syngas to a tar separation unit and obtain a warm syngas; and e. supply the warm syngas to the fermenter.
  • the warm syngas from the thermo-chemical process is preferably supplied to a recirculation pipe of the fermenter and is mixed with recirculating headspace gas and/or the warm syngas and the feedstock is supplied to an inline mixer.
  • Figure 1 depicts a first embodiment of the process according to the invention
  • Figure 2 depicts a preferred embodiment of the fermenter according to the invention
  • FIG. 3 depicts a detail of the thermo-chemical process according to the invention
  • Figure 4 depicts a second preferred embodiment of the process according to the invention for including digestate in the thermo-chemical process feedstocks
  • Figure 5 depicts a third preferred embodiment of the process according to the invention for production of hydrogen and biochar
  • Figure 1 is a flow diagram showing the first embodiment of the process according to present invention.
  • a wet feedstock (2) which can be either garden waste, sawdust, bark, or plastic-containing wastes, and is dried in a dryer (14).
  • the dried feedstock (3) is then mixed with a dry feedstock (20), which can be either demolition wood, white pellet, or black pellet, and pretreated in a pretreatment unit (38).
  • the pretreatment unit (38) is used to produce a homogenous, high bulky density feed to downstream processes.
  • the mixed feedstock (7) is then sent to a thermo-chemical process (15).
  • thermo-chemical process Inside the thermo-chemical process (15) (see also Fig. 3 showing a more detailed view of the thermo-chemical process (15)), the mixed feedstock (7) is first mixed with a headspace gas (10) from a fermenter (11 ) in a feed chamber (36).
  • the headspace gas (10) acts as carrier gas in the thermo-chemical process (15).
  • the mixture After the feed chamber (36), the mixture enters a thermo-chemical unit (17), which is typically operated at a temperature between 250-850 °C, at atmospheric pressure and under a low oxygen environment.
  • thermo-chemical process (15) can include processes such as pyrolysis, gasification, and torrefaction.
  • the thermo-chemical unit (17) can be heated by a high temperature gas (26) or by electricity or by heat released from the mixed feedstock (7) or combinations of thereof.
  • the high temperature gas (26) can be flue gas by burning biogas, biomethane, natural gas, biomass, or other energy materials.
  • thermo chemical unit (17) the mixed feedstock (7) is converted into a char fraction (23) and a hot syngas (25).
  • the solid char (23) comes out at the bottom of the thermo-chemical unit (17) via an airlock (37) by gravity and the hot syngas (25) comes out on the top of the thermo-chemical unit (17).
  • the solid char (23) itself has a moisture content less than 1% but can be damped with water to reduce dust production during char cooling and transportation.
  • the solid char (23) has a fixed carbon content of 20-90 wt-%.
  • the hot syngas (25) is then separated in a tar separation unit (18) to produce a warm syngas (8) and a tar (24).
  • a warm syngas (8) enters a fermenter (1 1 ).
  • the tar (24) is collected in a tar collection tank (28) and then either recirculated back to the inlet of the thermo-chemical unit (17) for volume reduction or used as raw material in another process, such as for heat production, transport fuel production in a refinery, as binding agent, or chemical production.
  • the tar (24) can have the same inlet with the mixed feedstock (7) or a different inlet to the thermo-chemical unit (17).
  • the heat exchanging unit (35) can in one embodiment be placed externally of the tar separation unit (18) and in this embodiment, the heat exchanging unit (35) can be placed either upstream or downstream of the tar separation unit (18).
  • the heat loss in the heat exchanger (35) can be partially recovered and used in the overall process, such as for heating an AD feedstock (1 ).
  • the high temperature gas (26) can be used periodically to clean the tar separation unit.
  • the AD feedstock (1 ) which is typically pretreated food waste, biological sludge, manure, slaughterhouse waste or combined more than one of the four, is led into the fermenter (11 ) where the AD feedstock (1 ) is mixed with the warm syngas (8) from the thermo-chemical process (15). In the fermenter (11 ), biological reactions occur under a temperature between 45-70 °C, a pressure of 1 -7 bar and a pH of 4.0-6.0.
  • Digestate (5) from a digester (12) can be added into the fermenter (11 ) during system start-ups for inoculation.
  • Organics in the AD feedstock (1 ) and the warm syngas (8) are converted to small molecular, water soluble compounds via a series of biological reactions including fermentation, hydrolysis, acidogenesis, fermentative hydrogen production, acetogenesis, homo-acetogenesis and methanogenesis.
  • a large portion of the warm syngas (8) mainly hydrogen, carbon monoxide, and carbon dioxide
  • the methanogenesis reactions are intentionally suppressed in the fermenter (11 ) by applying operating pressures including temperatures, pH and hydraulic retention times to methanogenesis microorganisms, which will facilitate the conversion of the warm syngas (8) into water soluble compounds.
  • the fermenter (11 ) is shown in more details in Fig. 2.
  • the warm syngas (8) enters the fermenter (11 ) in two ways.
  • One way is to inject the warm syngas (8) in a recirculation pipe (39) where headspace gas (10) is circulated to stir the mixture in the fermenter (11 ).
  • a pump (31 ) is used to regulate the headspace gas (10) recirculation rates.
  • the other way is to mix the warm syngas (8) and the feedstock (1 ) in an in-line mixer (16) and then the mixture is pumped into the fermenter (11 ) via another pump (32).
  • the solid char (23) can be added into the fermenter (11 ) at a percentage of 0.5-10% to the AD feedstock (1 ) volume to improve the fermenter (11 ) and the downstream digester (12) performance.
  • the process can use either one of the two ways or both ways combined.
  • the warm syngas (8) can be mixed into the headspace gas (10) and in another embodiment, the warm syngas (8) can be injected via the in-line mixer (16). It is also conceivable to split the warm (8) syngas into two streams and combine these two embodiments.
  • a mechanical mixer (33) can be used (as an option) to obtain an ideal mixing condition in the fermenter (11).
  • Internal structures, such as bundles of plastic carriers, can be added in the fermenter
  • the fermenter (11 ) to help increase gas-liquid mass transfer by shearing gas bubbles and to provide high surface areas for biofilm formation.
  • the fermenter (11 ) can have different shapes such as cylinder or rectangular.
  • the fermenter (11 ) has typical height-to-diameter ratios of 1.5-10.
  • the digester (12) Periodically, part of the deposit (9) in the fermenter (11 ) is removed from the fermenter (11 ).
  • the digester (12) has a larger volume than the fermenter
  • the digester (12) can be either wet digester (dry matter content of the digester content ⁇ 15 wt-%) or dry digester (dry matter content of the digester content > 15 wt-%).
  • Biogas (21 ) and digestate (5) are produced in the digester (12) via a series of biological reactions including fermentation, hydrolysis, acidogenesis, fermentative hydrogen production, acetogenesis, homo-acetogenesis and methanogenesis. The methanogenesis reaction is intentionally encouraged in the digester (12).
  • the headspace gas (10) from the fermenter (11 ) first enters a gas buffer tank (29) before it is split into two streams.
  • One stream enters the thermochemical process and functions as carrier gas.
  • the other stream enters a second thermo-chemical process (19) and functions as fuel.
  • the split ratio (the flow to the thermo-chemical process (15) versus the flow to the second thermochemical process (19)) varies between 1 to 20.
  • the second thermo-chemical process (19) can be a hydrogen production (via methane reforming reactions, water-gas-shift reactions, chemical looping reforming reactions, or combinations thereof) process or a heat production (combustion) process.
  • the biogas (21 ) can be optionally introduced into the second thermo-chemical process as additional fuel.
  • the digestate (5) is first dewatered in a dewatering unit (13) to separate reject water (22) and dewatered digestate (6). Ammonia recovery from the reject water (22) is typically applied before it is treated in a wastewater treatment unit.
  • the dewatered digestate (6) is mixed with the wet feedstock (2) to be dried in the dryer (14). In this way, the organic residue in the dewatered digestate (6) can be further processed in the thermo-chemical process (15).
  • the slurry (4) from the fermenter (11 ) can be sent to the dewatering unit (13) directly. After dewatering, the dewatered slurry (6) is dried in the dryer (14) and then thermo-chemically treated in the thermochemical process (15). The headspace gas (10) from the fermenter (11 ) enters the second thermo-chemical process (19) for hydrogen or heat production.
  • the present invention has following advantages by combining the features presented above:
  • the design of the fermenter (11 ) serves a main function of converting the syngas (8) to water soluble compounds.
  • the pH values, the pressures in the fermenter, the temperatures, the headspace circulation pipe (39), the gas distribution system (34), the feed distribution system (30), and the internal structure of the fermenter are all designed for optimizing the syngas conversion to water soluble compounds.
  • the methanogenesis reactions in the fermenter (11 ) are intentionally suppressed, which helps to increase the syngas conversion efficiency.
  • the headspace gas (10) is enriched with nitrogen and methane, which cannot be converted to water soluble compounds, and traces of convertible gases, such as carbon dioxide, hydrogen, and carbon monoxide, which remains in the headspace gas. It is not a good practice to introduce the nitrogen-containing headspace gas to an anaerobic digester since nitrogen is a contaminant in biogas, which either reduces biogas calorific value or generates additional costs for nitrogen separation when purified biogas (biomethane) is the final product.
  • the headspace gas is separated from the slurry (4) in the fermenter (11 ) and only the slurry (4) enters the digester (12).
  • the headspace due to its nitrogen content, is valuable for the thermo-chemical process (15) as carrier gas.
  • an oxygen-free carrier gas such as nitrogen
  • a commercial carrier gas can be costly to the thermo-chemical process operation.
  • Using the headspace gas (10), which is rich in nitrogen and free of oxygen, as carrier gas improves the thermo-chemical process performance and meantime, reduces the operational costs.
  • Methane is an ingredient in the syngas (8) and cannot be converted to water soluble compounds in the fermenter (11 ) and will be enriched in the headspace gas (10).
  • the enriched methane content will help to shift the reaction kinetics towards more hydrogen production in the process, which will eventually help to increase biogas production in the digester (12).
  • the headspace gas can also exit the system by entering the second thermochemical process (19) and its calorific value in methane, hydrogen and carbon monoxide residues can be valorized into heat or into hydrogen.
  • Some condensable organics in the syngas (8) are also converted to water soluble compounds in the fermenter (11 ). These organics are in the gaseous forms at high temperatures (70-320 °C) and become a part of the slurry in the fermenter (temperatures 45-70 °C), which will be converted to biogas and digestate in the digester (12).
  • the sensible heat in the syngas (8) is also used to raise the temperature of the fermenter (11 ) which also receives the low temperature AD feedstock (1 ).
  • the sensible heat in the hot syngas (25) and from the second thermo-chemical process (19) can also be used to raise the temperature of the fermenter (11 ).
  • the heat required by the dryer (14) can also be supplied by the heat produced in the second thermo-chemical process (19).
  • the tar separation unit (18) separates the tar (24) from the warm syngas (8) and the tar (18) is handled separately.
  • the warm syngas which contains non-condensable gas, aqueous pyrolysis liquid (in gaseous form at the presented temperatures), and a part of bio-oil (in gaseous form at the presented temperatures), can enter the fermenter (11 ) and then the digester (12) for biogas production.
  • the present invention can potentially minimize the tar (24) production and maximize the warm syngas production, which will lead to high biogas production.
  • Digestate depending on feedstock compositions, may contain microplastics or pharmaceutical residues or both, which makes it less valuable.
  • biogas plants will be able to remove the microplastics and the pharmaceutical residues in the digestate and produce additional biogas and biochar, which have high values in circular economy.
  • the biochar (23), as an option, is added into the fermenter (11 ) and the digester (12) to improve system performance by raising slurry alkalinity and providing high surface area for biofilm formation.
  • the presented invention can solve a wide range of environmental issues and unlock an enormous amount of unconventional feedstocks for biogas production, produce different types of biochar for a wide range of biochar applications, and generate multiple forms of renewable energy: biogas, thermal, and hydrogen.

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Abstract

La présente invention concerne un procédé de traitement de déchets organiques, ledit procédé comprenant les étapes suivantes : i) fourniture d'une charge humide (2) comprenant des déchets organiques à un séchoir (14) et obtention d'une charge séchée (3) ; ii) mélange et prétraitement de la charge séchée (3) avec une charge sèche (20) comprenant des déchets organiques pour obtenir une charge mixte (7) ; iii) fourniture de la charge d'alimentation mixte (7) à un processus thermochimique (15) et obtention d'une fraction de charbon (23) et d'un gaz de synthèse chaud (25) ; iv) décharge de la fraction de charbon (23) et séparation du flux de gaz de synthèse chaud (25) en gaz de synthèse chaud (8) et en goudron (24) dans une unité de séparation du goudron (18) ; v) fourniture d'une charge d'alimentation AD (1) et du gaz de synthèse chaud (8) de l'unité de séparation des goudrons (18) à un fermenteur (11) et exposition de la charge d'alimentation AD (1) et du gaz de synthèse chaud (8) à une série de réactions biologiques pour obtenir un gaz de l'espace libre (10) et une boue (4) dans le fermenteur (11) ; vi) fourniture de la boue (4) du fermenteur (11) à un digesteur (12) et exposition de la boue (4) à une série de réactions biologiques pour obtenir du biogaz (21) et un digestat (5) ; vii) fourniture d'une partie du gaz de l'espace de tête (10) du fermenteur (11) au processus thermochimique (15) comme gaz porteur pour la production de gaz de synthèse et fourniture du reste du gaz de l'espace de tête (10) du fermenteur (11) à un second processus thermochimique (19) comme combustible pour la production d'énergie.
PCT/NO2022/050200 2021-08-24 2022-08-23 Procédé de traitement de déchets organiques et de récupération de ressources Ceased WO2023027590A1 (fr)

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US12196412B2 (en) 2019-05-07 2025-01-14 Kore Infrastructure Production of renewable fuel for steam generation for heavy oil extraction
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US12196412B2 (en) 2019-05-07 2025-01-14 Kore Infrastructure Production of renewable fuel for steam generation for heavy oil extraction
WO2024226948A1 (fr) * 2023-04-27 2024-10-31 Kore Infrastructure, Llc Production de combustible renouvelable à partir de déchets chargés de nutriments par un procédé à teneur réduite en carbone
DE102024111304A1 (de) * 2024-04-17 2025-10-23 Andreas Simon Biomasseanlage und Verfahren zum Betreiben einer Biomasseanlage

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