WO2024084019A1 - Waste processing system and method - Google Patents

Waste processing system and method Download PDF

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Publication number
WO2024084019A1
WO2024084019A1 PCT/EP2023/079227 EP2023079227W WO2024084019A1 WO 2024084019 A1 WO2024084019 A1 WO 2024084019A1 EP 2023079227 W EP2023079227 W EP 2023079227W WO 2024084019 A1 WO2024084019 A1 WO 2024084019A1
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WO
WIPO (PCT)
Prior art keywords
waste product
optionally
thermal converter
gasification chamber
waste
Prior art date
Application number
PCT/EP2023/079227
Other languages
French (fr)
Inventor
Michael Burns
Original Assignee
Clean Thermodynamic Energy Conversion Ltd
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Filing date
Publication date
Application filed by Clean Thermodynamic Energy Conversion Ltd filed Critical Clean Thermodynamic Energy Conversion Ltd
Publication of WO2024084019A1 publication Critical patent/WO2024084019A1/en

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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
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • B09B3/45—Steam treatment, e.g. supercritical water gasification or oxidation
    • 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
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
    • 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
    • C02F11/06—Treatment of sludge; Devices therefor by oxidation
    • C02F11/08—Wet air oxidation
    • C02F11/086—Wet air oxidation in the supercritical state
    • 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/002—Horizontal gasifiers, e.g. belt-type gasifiers
    • 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
    • C10K3/001—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 thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/006—Reducing the tar content by steam reforming
    • 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
    • B09B2101/25—Non-industrial waste, e.g. household 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
    • 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
    • B09B2101/80—Rubber waste, e.g. scrap tyres
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • C02F1/004—Processes for the treatment of water whereby the filtration technique is of importance using large scale industrial sized filters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/36—Organic compounds containing halogen
    • 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
    • C10J2300/0923—Sludge, e.g. from water treatment plant
    • 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
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0979—Water as supercritical steam
    • 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
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1612—CO2-separation and sequestration, i.e. long time storage
    • 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/005—Carbon dioxide

Definitions

  • the present invention relates to a waste processing system for and method of processing waste product, such as municipal solid waste (MSW) and processed waste, for exampie, refuse-derived waste (RDF), including human waste, waste which contains organofluorines, such as perfluorocarbons (PFCs), including perfluoroalkyl and polyfluoroalkyl substances (PFAS), such as perfluorooctanoic acid (PFOA), perfluorooctanesulfonic acid (PFOS) and perfluorohexane sulfonic acid (PFHxS), and also fluorinated gases (F-gases).
  • the waste product can be a solid, liquid or gas, or combinations thereof, and can be supplied in many forms, for example, sludge, plastic and biomass, and includes tires and flooring material and tiles.
  • PFAS are substances having a chain of linked carbon and fluorine atoms, and, because the carbon-fluorine bond is one of the strongest, these substances are recalcitrant and not easily degraded.
  • Waste product typically contains a significant percentage of water, which gives rise to problems in processing, especially in systems using high- temperature combustion.
  • the present inventors have, however, recognized that this contained water can advantageously be employed in processing of the waste product itself, in that, if the contained water is extracted to generate supercritical water, this supercritical water can be utilized for supercritical water oxidation (SCWO), which has been found to reduce the PFAS content by greater than 99% (Krause et al, Supercritical Water Oxidation as an Innovative Technology for PFAS Destruction, Journal of Environmental Engineering, 148, 10.1061/(ASCE)EE.1943-7870.0001957).
  • SCWO supercritical water oxidation
  • the PFAS content of the waste product would otherwise have to be converted thermally at high temperature, typically above 1200 C, and moisture arising from water in the waste product would have to be carefully regulated.
  • the present invention provides a waste processing system, comprising: a drying chamber which includes a cavity which is supplied with waste product and heated to dry the waste product and generate steam, optionally flash steam; and a treatment unit which is fluidly connected to the drying chamber, wherein the treatment unit treats the steam received from the drying chamber to generate supercritical water, and includes an oxidant supply which supplies an oxidant, optionally air, to the generated supercritical water, whereby the treatment unit provides for supercritical water oxidation of waste substance.
  • the present invention provides a method of processing waste product, comprising: heating waste product in a drying chamber to generate steam, optionally flash steam; treating the steam which is received from the drying chamber in a treatment unit to generate supercritical water; and supplying an oxidant, optionally air, to the generated supercritical water to cause supercritical water oxidation of waste substance.
  • FIG. 1 illustrates a waste processing system in accordance with one embodiment of the present invention
  • Figure 2 illustrates a horizontal sectional view (along section I-I in Figure 1) of the system of Figure 1;
  • FIG. 3 illustrates an exhaust gas treatment system in accordance with one embodiment of the present invention.
  • Figure 4 represents the reduction in carbon dioxide emission to the atmosphere using the exhaust gas treatment system of Figure 3.
  • FIGS 1 and 2 illustrate a waste processing system in accordance with one embodiment of the present invention.
  • the system comprises a primary waste product supply 3 for supplying waste product, a secondary waste product supply 5 for supplying waste product, a drying chamber 7 which is supplied with the waste product from the primary waste product supply 3 and heats the waste product to dry the waste product and generate steam, a gasification chamber 9 which receives the waste product from the drying chamber 7 and in which the waste product is heated to generate synthetic gas or syngas, a treatment unit 11 for treating steam vented from the drying chamber 7, and a thermal converter 12 for generating a stream of heated gas for energy conversion.
  • the waste product is municipal solid waste (MSW) or processed waste, for example, refuse-derived waste (RDF), including human waste.
  • MSW municipal solid waste
  • RDF refuse-derived waste
  • the waste product contains organofluorines, such as perfluorocarbons (PFCs), including perfluoroalkyl and polyfluoroalkyl substances (PFAS), for example, perfluorooctanoic acid (PFOA), perfluorooctanesulfonic acid (PFOS) and perfluorohexane sulfonic acid (PFHxS).
  • organofluorines such as perfluorocarbons (PFCs), including perfluoroalkyl and polyfluoroalkyl substances (PFAS), for example, perfluorooctanoic acid (PFOA), perfluorooctanesulfonic acid (PFOS) and perfluorohexane sulfonic acid (PFHxS).
  • PFCs perfluorocarbons
  • PFAS perfluoroalkyl and polyfluoroalkyl substances
  • PFOA perfluorooctanoic acid
  • PFOS perfluoro
  • the waste product contains fluorinated gases (F-gases).
  • the waste product comprises a solid, liquid or gas, or combinations thereof.
  • the waste product is supplied in many forms, for example, sludge, plastic and biomass, and includes tires and flooring material and tiles.
  • the primary waste product supply 3 comprises a container 15, here in the form of a hopper, which contains waste product, in one embodiment in the form of a solid or sludge or mixtures thereof, and a waste feed 17 which feeds waste product from the container 15 to the drying chamber 7.
  • the waste feed 17 comprises a ram 19 which is actuated reciprocally between a first, material-receiving position, in which waste product can fall from the container 15 in front of the ram 19, and a second, feed position, in which the waste product ahead of the ram 19 is fed, here pushed, into an upstream end of the drying chamber 7.
  • the feeding of fresh waste product into the drying chamber 7 causes waste product at a downstream end of the drying chamber 7 to be fed into an upstream end of the gasification chamber 9.
  • the drying chamber 7 comprises an elongate cavity 21 along which waste product is displaced with operation of the waste feed 17.
  • the drying chamber 7 includes a heated gas source 23 which supplies a heated gas into the cavity 21 thereof, which heated gas can be a recirculated exhaust gas, and an outlet 24, here including a plurality of vents 26, through which steam, in this embodiment flash steam, is vented from the drying chamber 7.
  • a heated gas source 23 which supplies a heated gas into the cavity 21 thereof, which heated gas can be a recirculated exhaust gas, and an outlet 24, here including a plurality of vents 26, through which steam, in this embodiment flash steam, is vented from the drying chamber 7.
  • the temperature of the drying chamber 7 is controlled such that the upstream end of the cavity 21 is maintained at a temperature of less than 600 C, which is sufficient to yield steam from the moisture within the waste product.
  • the treatment unit 11 heats the steam which is received from the drying chamber 7 to a temperature above 374 C and a pressure above 22.1 MPa, which represents the critical point, in order to generate supercritical water.
  • the treatment unit 11 includes an inlet 27 which is fluidly connected to the outlet 24 of the drying chamber 7 and an outlet 28 which is fluidly connected to the thermal converter 12.
  • the treatment unit 11 includes a heated gas source 29 which supplies a heated gas to the treatment unit 11 to heat the received steam, which heated gas can be a recirculated exhaust gas.
  • the treatment unit 11 includes a reactor 30, which generates supercritical water from the received steam.
  • the treatment unit 11 includes an oxidant supply 31 which supplies an oxidant, here air, to the generated supercritical water.
  • an oxidant here air
  • the supercritical water provides for supercritical water oxidation of material, here in the thermal converter 12, which, as noted above, has been found to reduce the PFAS content by greater than 99%.
  • the gasification chamber 9 comprises a cavity 33 having an outlet 34, here in an upper section thereof, and a floor assembly 35, here at lower section thereof, over which waste product is transferred.
  • the floor assembly 35 comprises a transfer mechanism 39 which provides a grate at the floor of the gasification chamber 9 and transfers waste product which is received from the drying chamber 7 through a gasification zone GZ.
  • the transfer mechanism 39 comprises a stepped assembly 45 over which waste product is transferred.
  • the stepped assembly 45 comprises a plurality of steps 47, here of fixed position, which are arranged in staggered downward relation, and a plurality of movable members 49 which are movable reciprocally in relation to the steps 47 to transfer waste product along and over the steps 47.
  • the steps 47 are arranged substantially in spaced, parallel relation, and the movable members 49 are configured such that upper and lower surfaces of the movable members 49 are in close relation to adjacent surfaces of the steps 47, whereby the action of withdrawing the movable members 49 acts to scrape material therefrom.
  • ones or groups of ones of the movable members 49 are movable independently of one another, so as to enable control of an amount of waste product in the gasification zone GZ. This manner of control allows readily for use with different kinds of waste product, with the rate of transfer being controlled accordingly.
  • the gasification chamber 9 includes a heated gas source 51 which supplies a heated gas to the gasification chamber 9, which heated gas can be a recirculated exhaust gas, and heats the waste product to generate synthetic gas or syngas, with the temperature within the gasification zone GZ being controlled so as to prevent combustion, here to a temperature of less than 600 C.
  • the heated gas source 51 supplies the heated gas to the gasification chamber 9 through the transfer mechanism 39.
  • the gasification chamber 9 includes a combustion zone CZ at a downstream region thereof, at which a temperature is maintained to provide for starved combustion of the waste product thereat, which waste product has passed through the gasification zone GZ and from which syngas has been extracted.
  • the gasification chamber 9 includes a flow restrictor 55, here in the form of an apertured refractory member, at the outlet 34 thereof through which the flow of the generated syngas and heated gas is restricted, in order to provide for controlled generation and supply of syngas from the gasification chamber 9.
  • a flow restrictor 55 here in the form of an apertured refractory member, at the outlet 34 thereof through which the flow of the generated syngas and heated gas is restricted, in order to provide for controlled generation and supply of syngas from the gasification chamber 9.
  • thermal converter 12 is fluidly connected to the outlets 28, 34 of the treatment unit 11 and the gasification chamber 9.
  • outlet 28 of the treatment unit 11 is fluidiy connected to the thermal converter 12 downstream of the outlet 34 of the gasification chamber 9.
  • the thermal converter 12 includes an elongate cavity 71, with the outlet 34 of the gasification chamber 9 being located at an upstream region of the cavity 71.
  • the thermal converter 12 includes a flow accelerator 73 which is fluidly connected to the outlet 34 of the gasification chamber 9 and acts to provide a flow of syngas of increased velocity from the gasification chamber 9.
  • the thermal converter 12 includes a burner 75 which acts to ignite and provide for burning of the syngas as delivered from the gasification chamber 9, and a suction fan 77 which acts to draw the syngas into the cavity 71 of the thermal converter 12.
  • suction fan 77 is regulated to control temperature and residence time within the thermal converter 12.
  • the thermal converter 12 is controlled such that a temperature of at least 1000 C, in one embodiment at least 1100 C, is maintained in the cavity 71 thereof. In this embodiment the temperature within the cavity 71 of the thermal regulator 12 is maintained at a temperature of less than 1400 C.
  • the secondary waste product supply 5 comprises a container 81, here in the form of a chamber, which contains waste product, in one embodiment in the form of a particulate, liquid or gas or mixtures thereof, and a waste feed 83 which feeds waste product from the container 81 into the cavity 71 of the thermal converter 12.
  • the container 81 is adapted separately to contain particulate, liquid and gas or mixtures thereof.
  • the waste feed 83 comprises one or more injectors 85.
  • the thermal converter 12 in addition to generating a stream of heated gas for energy conversion, acts further to destroy substances which are delivered in the gas flow from the gasification chamber 9, including residual hydrocarbons, organofluorines and fluorinated gases, and also waste product which is delivered directly by the secondary waste product supply 5 into the cavity 71 of the thermal converter 12.
  • FIG. 3 illustrates an exhaust gas treatment system in accordance with one embodiment of the present invention.
  • the exhaust gas treatment system comprises a carbon dioxide scrubber 101 which receives an exhaust gas, in this embodiment from the waste treatment system of the above-described embodiment, and an absorbent, which acts to remove carbon dioxide and residual pollutants from the exhaust gas, an absorbent supply 103 for supplying absorbent to the scrubber 101, and a carbon dioxide reformer 105 which receives the carbon dioxide-rich absorbent from the scrubber 101 and reforms the absorbent and yields carbon dioxide for capture.
  • the scrubber 101 is a cyclone scrubber.
  • the absorbent is provided as a spray.
  • the absorbent is an aqueous absorbent.
  • the absorbent is an amine
  • the absorbent is monoethanolamine (MEA).
  • the reformer 105 reforms the carbon-dioxide absorbent by steam reforming to boil the absorbent, here with steam supplied from the waste treatment system, and yields carbon dioxide for capture, with the lean, reformed absorbent being recirculated to the absorbent supply 103.
  • system further comprises a carbon dioxide extraction unit 107, which extracts carbon dioxide from the reformer 105 under vacuum and compresses the extracted carbon dioxide for recycling.
  • system further comprises a filtration unit 109, which receives the residual water from the reformer 105 and filters residual pollutants therefrom.
  • the present inventors have recognized that, by utilizing steam, as an available by-product of the waste processing system, much reduced consumption of the absorbent can be achieved and the captured carbon dioxide can be recycled to provide a usable source of carbon dioxide.
  • the secondary waste product supply 5 could be omitted.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Hydrology & Water Resources (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Drying Of Solid Materials (AREA)
  • Drying Of Gases (AREA)

Abstract

A waste processing system and method, the waste processing system comprising: a drying chamber (7) which includes a cavity (21) which is supplied with waste product and heated to dry the waste product and generate steam, optionally flash steam; and a treatment unit (11) which is fluidly connected to the drying chamber (7), wherein the treatment unit (11) treats the steam received from the drying chamber (7) to generate supercritical water, and includes an oxidant supply (31) which supplies an oxidant, optionally air, to the generated supercritical water, whereby the treatment unit (11) provides for supercritical water oxidation of waste substance.

Description

WASTE PROCESSING SYSTEM AND METHOD
The present invention relates to a waste processing system for and method of processing waste product, such as municipal solid waste (MSW) and processed waste, for exampie, refuse-derived waste (RDF), including human waste, waste which contains organofluorines, such as perfluorocarbons (PFCs), including perfluoroalkyl and polyfluoroalkyl substances (PFAS), such as perfluorooctanoic acid (PFOA), perfluorooctanesulfonic acid (PFOS) and perfluorohexane sulfonic acid (PFHxS), and also fluorinated gases (F-gases). The waste product can be a solid, liquid or gas, or combinations thereof, and can be supplied in many forms, for example, sludge, plastic and biomass, and includes tires and flooring material and tiles.
PFAS are substances having a chain of linked carbon and fluorine atoms, and, because the carbon-fluorine bond is one of the strongest, these substances are recalcitrant and not easily degraded.
Waste product typically contains a significant percentage of water, which gives rise to problems in processing, especially in systems using high- temperature combustion. The present inventors have, however, recognized that this contained water can advantageously be employed in processing of the waste product itself, in that, if the contained water is extracted to generate supercritical water, this supercritical water can be utilized for supercritical water oxidation (SCWO), which has been found to reduce the PFAS content by greater than 99% (Krause et al, Supercritical Water Oxidation as an Innovative Technology for PFAS Destruction, Journal of Environmental Engineering, 148, 10.1061/(ASCE)EE.1943-7870.0001957). The PFAS content of the waste product would otherwise have to be converted thermally at high temperature, typically above 1200 C, and moisture arising from water in the waste product would have to be carefully regulated.
In one aspect the present invention provides a waste processing system, comprising: a drying chamber which includes a cavity which is supplied with waste product and heated to dry the waste product and generate steam, optionally flash steam; and a treatment unit which is fluidly connected to the drying chamber, wherein the treatment unit treats the steam received from the drying chamber to generate supercritical water, and includes an oxidant supply which supplies an oxidant, optionally air, to the generated supercritical water, whereby the treatment unit provides for supercritical water oxidation of waste substance.
In another aspect the present invention provides a method of processing waste product, comprising: heating waste product in a drying chamber to generate steam, optionally flash steam; treating the steam which is received from the drying chamber in a treatment unit to generate supercritical water; and supplying an oxidant, optionally air, to the generated supercritical water to cause supercritical water oxidation of waste substance.
Preferred embodiments of the present invention will now be described hereinbelow by way of example only with reference to the accompanying drawings, in which:
Figure 1 illustrates a waste processing system in accordance with one embodiment of the present invention;
Figure 2 illustrates a horizontal sectional view (along section I-I in Figure 1) of the system of Figure 1;
Figure 3 illustrates an exhaust gas treatment system in accordance with one embodiment of the present invention; and
Figure 4 represents the reduction in carbon dioxide emission to the atmosphere using the exhaust gas treatment system of Figure 3.
Figures 1 and 2 illustrate a waste processing system in accordance with one embodiment of the present invention. The system comprises a primary waste product supply 3 for supplying waste product, a secondary waste product supply 5 for supplying waste product, a drying chamber 7 which is supplied with the waste product from the primary waste product supply 3 and heats the waste product to dry the waste product and generate steam, a gasification chamber 9 which receives the waste product from the drying chamber 7 and in which the waste product is heated to generate synthetic gas or syngas, a treatment unit 11 for treating steam vented from the drying chamber 7, and a thermal converter 12 for generating a stream of heated gas for energy conversion.
In one embodiment the waste product is municipal solid waste (MSW) or processed waste, for example, refuse-derived waste (RDF), including human waste.
In one embodiment the waste product contains organofluorines, such as perfluorocarbons (PFCs), including perfluoroalkyl and polyfluoroalkyl substances (PFAS), for example, perfluorooctanoic acid (PFOA), perfluorooctanesulfonic acid (PFOS) and perfluorohexane sulfonic acid (PFHxS).
In one embodiment the waste product contains fluorinated gases (F-gases).
In one embodiment the waste product comprises a solid, liquid or gas, or combinations thereof.
In one embodiment the waste product is supplied in many forms, for example, sludge, plastic and biomass, and includes tires and flooring material and tiles.
In this embodiment the primary waste product supply 3 comprises a container 15, here in the form of a hopper, which contains waste product, in one embodiment in the form of a solid or sludge or mixtures thereof, and a waste feed 17 which feeds waste product from the container 15 to the drying chamber 7.
In this embodiment the waste feed 17 comprises a ram 19 which is actuated reciprocally between a first, material-receiving position, in which waste product can fall from the container 15 in front of the ram 19, and a second, feed position, in which the waste product ahead of the ram 19 is fed, here pushed, into an upstream end of the drying chamber 7. With this action of the ram 19, the feeding of fresh waste product into the drying chamber 7 causes waste product at a downstream end of the drying chamber 7 to be fed into an upstream end of the gasification chamber 9.
In this embodiment the drying chamber 7 comprises an elongate cavity 21 along which waste product is displaced with operation of the waste feed 17.
In this embodiment the drying chamber 7 includes a heated gas source 23 which supplies a heated gas into the cavity 21 thereof, which heated gas can be a recirculated exhaust gas, and an outlet 24, here including a plurality of vents 26, through which steam, in this embodiment flash steam, is vented from the drying chamber 7. With this configuration, the heated gas supplied to the drying chamber 7 and heat from the gasification chamber 9 acts to heat the waste product within the cavity 21 of the drying chamber 7.
In this embodiment the temperature of the drying chamber 7 is controlled such that the upstream end of the cavity 21 is maintained at a temperature of less than 600 C, which is sufficient to yield steam from the moisture within the waste product.
In this embodiment the treatment unit 11 heats the steam which is received from the drying chamber 7 to a temperature above 374 C and a pressure above 22.1 MPa, which represents the critical point, in order to generate supercritical water. In this embodiment the treatment unit 11 includes an inlet 27 which is fluidly connected to the outlet 24 of the drying chamber 7 and an outlet 28 which is fluidly connected to the thermal converter 12.
In this embodiment the treatment unit 11 includes a heated gas source 29 which supplies a heated gas to the treatment unit 11 to heat the received steam, which heated gas can be a recirculated exhaust gas.
In this embodiment the treatment unit 11 includes a reactor 30, which generates supercritical water from the received steam.
In this embodiment the treatment unit 11 includes an oxidant supply 31 which supplies an oxidant, here air, to the generated supercritical water. With the addition of oxidant, the supercritical water provides for supercritical water oxidation of material, here in the thermal converter 12, which, as noted above, has been found to reduce the PFAS content by greater than 99%.
In this embodiment the gasification chamber 9 comprises a cavity 33 having an outlet 34, here in an upper section thereof, and a floor assembly 35, here at lower section thereof, over which waste product is transferred.
In this embodiment the floor assembly 35 comprises a transfer mechanism 39 which provides a grate at the floor of the gasification chamber 9 and transfers waste product which is received from the drying chamber 7 through a gasification zone GZ.
In this embodiment the transfer mechanism 39 comprises a stepped assembly 45 over which waste product is transferred.
In this embodiment the stepped assembly 45 comprises a plurality of steps 47, here of fixed position, which are arranged in staggered downward relation, and a plurality of movable members 49 which are movable reciprocally in relation to the steps 47 to transfer waste product along and over the steps 47.
In this embodiment the steps 47 are arranged substantially in spaced, parallel relation, and the movable members 49 are configured such that upper and lower surfaces of the movable members 49 are in close relation to adjacent surfaces of the steps 47, whereby the action of withdrawing the movable members 49 acts to scrape material therefrom.
In this embodiment ones or groups of ones of the movable members 49 are movable independently of one another, so as to enable control of an amount of waste product in the gasification zone GZ. This manner of control allows readily for use with different kinds of waste product, with the rate of transfer being controlled accordingly.
In this embodiment the gasification chamber 9 includes a heated gas source 51 which supplies a heated gas to the gasification chamber 9, which heated gas can be a recirculated exhaust gas, and heats the waste product to generate synthetic gas or syngas, with the temperature within the gasification zone GZ being controlled so as to prevent combustion, here to a temperature of less than 600 C.
In this embodiment the heated gas source 51 supplies the heated gas to the gasification chamber 9 through the transfer mechanism 39.
In this embodiment the gasification chamber 9 includes a combustion zone CZ at a downstream region thereof, at which a temperature is maintained to provide for starved combustion of the waste product thereat, which waste product has passed through the gasification zone GZ and from which syngas has been extracted.
In this embodiment the gasification chamber 9 includes a flow restrictor 55, here in the form of an apertured refractory member, at the outlet 34 thereof through which the flow of the generated syngas and heated gas is restricted, in order to provide for controlled generation and supply of syngas from the gasification chamber 9.
In this embodiment the thermal converter 12 is fluidly connected to the outlets 28, 34 of the treatment unit 11 and the gasification chamber 9.
In this embodiment the outlet 28 of the treatment unit 11 is fluidiy connected to the thermal converter 12 downstream of the outlet 34 of the gasification chamber 9.
In this embodiment the thermal converter 12 includes an elongate cavity 71, with the outlet 34 of the gasification chamber 9 being located at an upstream region of the cavity 71.
In this embodiment the thermal converter 12 includes a flow accelerator 73 which is fluidly connected to the outlet 34 of the gasification chamber 9 and acts to provide a flow of syngas of increased velocity from the gasification chamber 9.
In this embodiment the thermal converter 12 includes a burner 75 which acts to ignite and provide for burning of the syngas as delivered from the gasification chamber 9, and a suction fan 77 which acts to draw the syngas into the cavity 71 of the thermal converter 12.
In this embodiment the suction fan 77 is regulated to control temperature and residence time within the thermal converter 12.
In this embodiment the thermal converter 12 is controlled such that a temperature of at least 1000 C, in one embodiment at least 1100 C, is maintained in the cavity 71 thereof. In this embodiment the temperature within the cavity 71 of the thermal regulator 12 is maintained at a temperature of less than 1400 C. In this embodiment the secondary waste product supply 5 comprises a container 81, here in the form of a chamber, which contains waste product, in one embodiment in the form of a particulate, liquid or gas or mixtures thereof, and a waste feed 83 which feeds waste product from the container 81 into the cavity 71 of the thermal converter 12.
In one embodiment the container 81 is adapted separately to contain particulate, liquid and gas or mixtures thereof.
In one embodiment the waste feed 83 comprises one or more injectors 85.
With this configuration, the thermal converter 12, in addition to generating a stream of heated gas for energy conversion, acts further to destroy substances which are delivered in the gas flow from the gasification chamber 9, including residual hydrocarbons, organofluorines and fluorinated gases, and also waste product which is delivered directly by the secondary waste product supply 5 into the cavity 71 of the thermal converter 12.
Figure 3 illustrates an exhaust gas treatment system in accordance with one embodiment of the present invention.
The exhaust gas treatment system comprises a carbon dioxide scrubber 101 which receives an exhaust gas, in this embodiment from the waste treatment system of the above-described embodiment, and an absorbent, which acts to remove carbon dioxide and residual pollutants from the exhaust gas, an absorbent supply 103 for supplying absorbent to the scrubber 101, and a carbon dioxide reformer 105 which receives the carbon dioxide-rich absorbent from the scrubber 101 and reforms the absorbent and yields carbon dioxide for capture.
In this embodiment the scrubber 101 is a cyclone scrubber. In one embodiment the absorbent is provided as a spray.
In this embodiment the absorbent is an aqueous absorbent.
In one embodiment the absorbent is an amine.
In this embodiment the absorbent is monoethanolamine (MEA).
In this embodiment the reformer 105 reforms the carbon-dioxide absorbent by steam reforming to boil the absorbent, here with steam supplied from the waste treatment system, and yields carbon dioxide for capture, with the lean, reformed absorbent being recirculated to the absorbent supply 103.
In this embodiment the system further comprises a carbon dioxide extraction unit 107, which extracts carbon dioxide from the reformer 105 under vacuum and compresses the extracted carbon dioxide for recycling.
In this embodiment the system further comprises a filtration unit 109, which receives the residual water from the reformer 105 and filters residual pollutants therefrom.
With this configuration, the present inventors have recognized that, by utilizing steam, as an available by-product of the waste processing system, much reduced consumption of the absorbent can be achieved and the captured carbon dioxide can be recycled to provide a usable source of carbon dioxide.
Use of the embodied exhaust gas treatment system in the above-described waste processing system avoids significant carbon dioxide emission to the atmosphere as compared to incineration, with the present embodiment typically yielding a reduction in the atmospheric carbon dioxide emission of greater than 80%, as represented in Figure 4. Finally, it will be understood that the present invention will be described in its preferred embodiments and can be modified in many different ways without departing from the scope of the present invention as defined by the appended claims.
For example, in the above-described waste processing system, the secondary waste product supply 5 could be omitted.

Claims

1. A waste processing system, comprising: a drying chamber (7) which includes a cavity (21) which is supplied with waste product and heated to dry the waste product and generate steam, optionally flash steam; and a treatment unit (11) which is fluidly connected to the drying chamber (7), wherein the treatment unit (11) treats the steam received from the drying chamber (7) to generate supercritical water, and includes an oxidant supply (31) which supplies an oxidant, optionally air, to the generated supercritical water, whereby the treatment unit (11) provides for supercritical water oxidation of waste substances.
2. The system of claim 1, wherein the cavity (21) is an elongate cavity along which waste product is displaced.
3. The system of claim 1 or 2, wherein the drying chamber (7) is supplied with a heated gas, optionally a recirculated exhaust gas, to heat the waste product.
4. The system of any of claims 1 to 3, wherein the treatment unit (11) is supplied with a heated gas, optionally a recirculated exhaust gas, to heat the received steam.
5. The system of any of claims 1 to 4, wherein the treatment unit (11) includes a reactor (30) which generates supercritical water from the received steam.
6. The system of any of claims 1 to 5, further comprising: a gasification chamber (9) which includes a cavity (33) which receives the waste product from the drying chamber (7) and in which the waste product is heated to generate synthetic gas or syngas within a gasification zone (GZ).
7. The system of claim 6, wherein the gasification chamber (9) includes a transfer mechanism (39) which transfers waste product which is received from the drying chamber (7) through the gasification zone (GZ).
8. The system of claim 6 or 7, wherein the gasification chamber (9) is supplied with a heated gas, optionally a recirculated exhaust gas, to heat the waste product.
9. The system of any of claims 6 to 8, wherein the gasification chamber (9) includes a combustion zone (CZ) at a downstream region thereof, at which a temperature is maintained to provide for starved combustion of the waste product thereat.
10. The system of any of claims 6 to 9, wherein the gasification chamber (9) includes a flow restrictor (55), optionally an apertured member, through which a flow of the generated syngas and heated gas is restricted.
11. The system of any of claims 6 to 10, further comprising: a thermal converter (12) which includes a cavity (71) and is fluidly connected to the treatment unit (11) and the gasification chamber (9) for generating a stream of heated gas for energy conversion, optionally the treatment unit (11) is fluidly connected to the thermal converter (12) downstream of the gasification chamber (9), optionally the cavity (71) is an elongate cavity, with the gasification chamber (9) being fluidly connected at an upstream region of the cavity (71).
12. The system of claim 11, wherein the thermal converter (12) includes a flow accelerator (73) which is fluidly connected to the gasification chamber (9) and acts to provide a flow of increased velocity from the gasification chamber (9).
13. The system of claim 11 or 12, wherein the thermal converter (12) includes a burner (75) which acts to ignite a flow of gas which is delivered from the gasification chamber (9), and a suction unit (77) which acts to draw the flow of gas into the thermal converter (12), with the suction unit (77) being regulated to control temperature and residence time within the thermal converter (12), optionally a temperature of at least 1000 C is maintained in the thermal converter (12), optionally a temperature of less than 1400 C is maintained in the thermal converter (12).
14. The system of any of claims 11 to 13, further comprising: a waste product supply (5) which feeds waste product into the cavity (71) of the thermal converter (12), optionally the waste product supply (5) comprises a container (81) which contains waste product, optionally in the form of a particulate, liquid or gas or mixtures thereof, and a waste feed (83) which feeds waste product from the container (81) into the cavity (71) of the thermal converter (12).
15. The system of any of claims 1 to 14, wherein the waste product includes one or both of organofluorines or fluorinated gases.
16. A method of processing waste product, comprising: heating waste product in a drying chamber (7) to generate steam, optionally flash steam; treating the steam which is received from the drying chamber (7) in a treatment unit (11) to generate supercritical water; and supplying an oxidant, optionally air, to the generated supercritical water to cause supercritical water oxidation of waste substances.
17. The method of claim 16, wherein the waste product is heated in the drying chamber (7) with a heated gas, optionally a recirculated exhaust gas.
18. The method of claim 16 or 17, wherein the steam which is received from the drying chamber (7) is heated with a heated gas, optionally a recirculated exhaust gas.
19. The method of any of claims 16 to 18, further comprising: transferring the waste product from the drying chamber (7) to a gasification chamber (9), optionally the waste product which is transferred from the drying chamber (7) is transferred through the gasification chamber (9); and heating the waste product within a gasification zone (GZ) of the gasification chamber (9) to generate synthetic gas or syngas, optionally a downstream region of the gasification chamber (9) is maintained at a temperature to provide for starved combustion of the waste product in a combustion zone (CZ).
20. The method of claim 19, wherein the waste product in the gasification chamber (9) is heated with a heated gas, optionally a recirculated exhaust gas.
21. The method of claim 19 or 20, further comprising: restricting a flow of the generated syngas and heated gas from the gasification chamber (9).
22. The method of any of ciaims 19 to 21, further comprising: providing output flows from the treatment unit (11) and the gasification chamber (9) to a cavity (71) of a thermal converter (12), optionaliy the output flow from the gasification chamber (9) is accelerated to provide a flow of increased velocity from the gasification chamber (9); and thermally converting material in the output flows which are received by the thermal converter (12) from the treatment unit (11) and the gasification chamber (9) to generate a stream of heated gas for energy conversion, optionally the treatment unit (11) is fluidly connected to the thermal converter (12) downstream of the gasification chamber (9).
23. The method of claim 22, further comprising: igniting the output flow from the gasification chamber (9) in the thermal converter (12); and regulating flow through the thermal converter (12) to control temperature and residence time within the thermal converter (12), optionally the flow through the thermal converter (12) is regulated by suction, optionally a temperature of at least 1000 C is maintained in the thermal converter (12), optionally a temperature of less than 1400 C is maintained in the thermal converter (12).
24. The method of claim 22 or 23, further comprising: feeding waste product directly into the cavity (71) of the thermal converter (12), optionally in the form of a particulate, liquid or gas or mixtures thereof.
25. The method of any of claims 16 to 24, wherein the waste product includes one or both of organofluorines or fluorinated gases.
PCT/EP2023/079227 2022-10-21 2023-10-20 Waste processing system and method WO2024084019A1 (en)

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