WO2012172329A2 - Appareil et procédé pour le traitement des déchets - Google Patents

Appareil et procédé pour le traitement des déchets Download PDF

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Publication number
WO2012172329A2
WO2012172329A2 PCT/GB2012/051335 GB2012051335W WO2012172329A2 WO 2012172329 A2 WO2012172329 A2 WO 2012172329A2 GB 2012051335 W GB2012051335 W GB 2012051335W WO 2012172329 A2 WO2012172329 A2 WO 2012172329A2
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WIPO (PCT)
Prior art keywords
autoclave
waste
steam
water
door
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Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
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PCT/GB2012/051335
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English (en)
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WO2012172329A3 (fr
Inventor
Ian Cecil Toll
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Aerothermal Group Ltd
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Aerothermal Group Ltd
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Publication date
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Publication of WO2012172329A2 publication Critical patent/WO2012172329A2/fr
Publication of WO2012172329A3 publication Critical patent/WO2012172329A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/28—Moving reactors, e.g. rotary drums
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/04—Pressure vessels, e.g. autoclaves
    • B01J3/042—Pressure vessels, e.g. autoclaves in the form of a tube
    • 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
    • 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
    • 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
    • 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
    • C02F11/18—Treatment of sludge; Devices therefor by thermal conditioning
    • 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
    • C12M43/00—Combinations of bioreactors or fermenters with other apparatus
    • 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
    • C12M45/20—Heating; Cooling
    • 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
    • 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
    • Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing

Definitions

  • This invention relates to apparatus for the treatment of solid waste and to the treatment of solid waste in the said apparatus.
  • a plant for treating solid waste comprising at least one autoclave for steam treating the waste, at least one anaerobic digestion tank for digesting an organic-rich fraction of the autoclaved waste, a recovery system for recovering methane-containing gas from the or each digestion tank, at least one internal combustion engine for combusting the methane-containing gas and generating power, and a steam generator fed with combustion gas from the internal combustion engine for generating and accumulating steam for supply to said at least one autoclave.
  • the invention provides apparatus for the treatment of solid waste comprising: autoclave treatment apparatus for steam treating the solid waste; and a supercritical water oxidation reactor downstream of the autoclave treatment apparatus for converting a product stream to water and carbon dioxide.
  • the above apparatus may comprise screening apparatus for separating a product stream from the autoclave treatment apparatus into a stream of organic-rich aqueous material and a reject stream of mechanically separable solids and the supercritical water oxidation reactor is arranged to receive the organic-rich aqueous stream and oxidise the organic material of said stream to water and carbon dioxide.
  • the above apparatus comprises screening apparatus for separating a product stream from the autoclave treatment apparatus into a stream of organic-rich aqueous material and a reject stream of mechanically separable solids and at least one anaerobic digestion tank for digesting the organic-rich aqueous material, wherein the supercritical water oxidation reactor is arranged to receive and oxidise sludge from the anaerobic digestion to water and carbon dioxide.
  • the invention further comprises a process for treating solid waste which comprises processing the waste in a plant as described above.
  • Fig 1 shows apparatus for the treatment of solid waste including autoclave treatment apparatus and a supercritical water oxidation reactor downstream of the autoclave treatment apparatus for converting an autoclave product stream to carbon dioxide and water;
  • Fig 2 shows apparatus for the treatment of solid waste including an autoclave, an anaerobic digestion plant for digesting a product stream of autoclaved material and a supercritical water oxidation reactor downstream of the autoclave treatment apparatus for converting sludge from the anaerobic digester to carbon dioxide and water;
  • Fig. 3 is a simplified oblique view from a lower end thereof of an autoclave and support structure, upper and lower doors being shown in their closed positions;
  • Fig. 4 is an oblique view of the autoclave of Fig 3 from its upper end, an upper door being shown in its open position;
  • Fig. 5 is a slightly oblique side view of the autoclave showing the lower door in its open position
  • Fig 6 is a further side view of the autoclave with both upper and lower doors open and with the autoclave viewed in longitudinal vertical section to reveal its internal flights.
  • Solid waste Wastes which may be treated by the method and apparatus of the invention include including but are not limited to municipal solid waste (MSW). Suitable waste will be normally classified as non-hazardous and non-toxic and may be at least in part biodegradable or may be wholly biodegradable. Its composition may depend on the extent of pre-sorting demanded by a municipality. It may include household waste or sorted fractions of household waste, catering waste (including waste from restaurants or other catering facilities), biodegradable supermarket waste, paper and biodegradable plastics waste, partly or wholly biodegradable commercial waste or mixtures thereof.
  • MSW Municipal solid waste
  • Suitable waste will be normally classified as non-hazardous and non-toxic and may be at least in part biodegradable or may be wholly biodegradable. Its composition may depend on the extent of pre-sorting demanded by a municipality. It may include household waste or sorted fractions of household waste, catering waste (including waste from restaurants or other catering facilities), biodegradable supermarket waste, paper and biodegradable plastics
  • non-biodegradable recyclable waste e.g. plastics, glass or a mixture thereof. It may also include specialised wastes such as animal and fish-based waste e.g. slaughterhouse waste, shellfish waste, poultry product waste and supermarket food waste.
  • Fig. 1 shows incoming waste 10 arriving at 12 at reception hall 14 leading to an autoclave and screening plant 24.
  • a recyclables stream 16 passes together with a stream recyclable discharge 20.
  • Potable water 26 is provided for autoclave treatment of the waste as described below.
  • a reject stream 28 from the autoclaves passes to landfill 22.
  • a screened organic fraction 32 from the autoclave plant 24 passes via slurry mixing tank 32 as stream 34 to dewatering plant 36 where it is mixed with flocculating agent 38.
  • An aqueous stream 40 from the dewatering plant passes to water treatment plant 42, with aqueous stream 44 being recycled to the autoclave and screening plant 24 and surplus effluent passing to supercritical water oxidation reactor 54.
  • Dewatered solids 48 pass to cake storage tank 50 and thence as stream 52 to the supercritical water oxidation reactor 54, where it is reacted with oxygen and converted to excess water stream 56, carbon dioxide stream 50 (the carbon dioxide being of value and optionally recovered) and steam stream 60 which is fed to turbine 62.
  • Electrical power from turbine 62 passes at 64 to the grid, and spent steam is recycled as stream 66 to the autoclave and screening plant 24.
  • the apparatus of Fig 2 is similar except that organic-rich stream 80 passes from the plant 24 to anaerobic digesters 82.
  • the resulting methane-containing gas passes as stream 84 to generators 86, steam boiler 90 and as exhaust stream 92 to atmosphere.
  • Process steam from boiler 90 passes as stream 92 to the autoclave and screening plant 24.
  • Digestate from the anaerobic digesters passes as stream 96 to digestate storage tank(s) 98 and thence as stream 100 to dewatering apparatus 23. Power to the grid comes both from generators 86 as 102 and from turbine 62 as 64.
  • the supercritical oxidation plant 54 may use air or oxygen as oxidant and additionally produces an inorganic solids-rich stream which may be centrifuged for removal of any residual inorganic products of the destruction of the organic material from the autoclaves or form anaerobic digestion. It is not excluded that the supercritical oxidiser may be configured to operate just below supercritical temperature e.g. intermittently.
  • the organic fraction is said to represent the industrial world's largest economically accessible source of lignocellulose feedstock for conversion into alcohol and other industrial chemicals. It is further explained that MSW is an environmental concern owing to the dwindling availability of landfill sites.
  • a treatment process is disclosed in which MSW is fed into a pressure vessel, subjected to heat at 132-160°C (270-320°F) under a pressure of from 276-517 kPa (40 to 75 psi) for 30-90 minutes with introduction of steam to give a residual moisture content of 60-70%, discharged and classified to give an organic fraction as fines with moisture content 60-70%.
  • US-A-4884351 discloses an autoclave for the handling of municipal solid waste which is in the form of a cylindrical vessel inclined at about 15° to the horizontal and having frustoconical ends each closed by a hinged hatch.
  • the hatch at the higher end serves as inlet for the waste to be processed and that at the lower end serves as an outlet for processed waste.
  • the autoclave is supported for rotation about its longitudinal axis and has internal flighting angled at about 30° to its axis by which in a forward rotation mode the fighting directs material to the lower end of the autoclave during filling and/or discharge and in a reverse rotation mode material being processed is conveyed upwardly and axially towards the higher end and is mixed and agitated, reverse rotation being during processing of the material.
  • Heating is by introduction of saturated steam via an inlet on the axis of the vessel and at the upper end thereof, the processing temperature being 48-108°C (120-228°F) preferably 88-102°C (190-215°F) to rupture bags of plastics film but to leave low density plastics materials substantially intact so that they are easily identifiable and separable from other components of the waste.
  • US-A-4974781 (Placzek) is similar and has as its object the re-pulping of re- pulpable waste material, the water content of the waste typically being 50 wt%.
  • Waste and water is added to a rotary autoclave or so-called "trommel" to give a moisture content of at least 30% of the moisture absorptive components of the waste, 65-75% moisture content being considered an optimum.
  • a working temperature of 100 - 115°C (212-240°F) is considered best for plastics recovery and 115-149°C is considered best for re-pulping.
  • the autoclave which in use is downwardly inclined at an angle of 4° is provided with lifting blades and directional flighting, a waste inlet at its upper end and a waste outlet at its lower end.
  • the inlet and outlet each have a closure device in the form of a sliding gate valve which is movable axially towards or away from the inlet or the outlet.
  • Steam and water can pass into the autoclave from its lower end via injection piping that extends into and rotates with the autoclave, the piping being connected to a rotary seal on the axis of rotation of the autoclave adjacent the discharge end.
  • running reliability of a rotary autoclave for MSW can be improved and the range of materials that can be effectively treated is improved by employing an autoclave having a fixed downwardly facing attitude and injecting steam through a port in a bottom discharge door of the autoclave.
  • a fixed attitude facilitates making the autoclave body or tunnel of material of adequate thickness not only to resist internal steam pressure but also to continue to do so if there is corrosion or erosion as a result of processing wet loads of MSW.
  • a commercial-scale autoclave of diameter e.g.
  • the autoclave body or tunnel may be formed of steel plate of significantly greater than the 9 mm steel plate as in other proposals e.g. 12-25 mm, the precise thickness depending e.g. on the dimensions of the autoclave or autoclaves proposed to be used.
  • the autoclave may face forwardly and downwardly at an angle of 5-20°, e.g. 10-15°, conveniently about 15°.
  • the door may be hinged to a support frame of said autoclave for rotational movement between one position in which a discharge opening of the autoclave is revealed and another position in which the discharge opening is closed.
  • the door carries a rotary coupling for receiving steam from a supply pipe as the autoclave is rotated.
  • a plenum chamber for steam in may be provided said door. Steam may be injected into the interior of the autoclave through a plurality of one-way devices providing parallel paths from the plenum chamber into the interior of the autoclave, thereby facilitating steam injection without undue pressure drop across the devices.
  • the cross-sectional area of the path or paths from the plenum chamber into the autoclave defined by said at least one-way device may be equal to or greater than the area of an inlet for injected steam into the plenum chamber.
  • Injecting the steam into the autoclave may be through at least one porous sintered metal disc leading from the plenum chamber into the autoclave or it may be through at least one mushroom or poppet valve or other one-way valve leading from the plenum chamber into the autoclave.
  • the autoclave may also have an inlet door for waste at its upper end, and an axially located inlet in said door for water to be sprayed into the autoclave to condense steam therein.
  • the door may be supported for hinged movement between open positions and a position spaced from and axially aligned with the discharge opening and is supported for translational movement between the spaced axially aligned position and the position in which the discharge opening is covered.
  • the method of treatment of the solid waste may include injecting steam from a steam accumulator having a capacity for a body of steam at a temperature and pressure effective to heat and fully penetrate the load and may also include injecting recycled steam from a second autoclave which has substantially completed its treatment cycle.
  • the autoclave has generally helical internal flights, and it is rotated during steam injection in a direction such that the flights lift the waste from the discharge end into the body of the autoclave.
  • Process control may include monitoring load at upper and lower ends of the autoclave while the flights are lifting the waste from the lower end, equalization of the load at the upper and lower ends compared to the loads at the end of waste introduction indicating that lifting is taking place.
  • Process control may further include monitoring pressure at upper and lower ends of the autoclave, substantial equality of pressure indicating that the steam has fully penetrated the load.
  • the processing time is considered to have started when the load has become fully penetrated by the steam/.
  • liquid water is introduced into the autoclave as the load is introduced, the water advantageously being near boiling and introduced in an amount of 25-100% based on the weight of the introduced load, e.g. 25-50 wt% based on the weight of the introduced load.
  • a yet further feature comprises spraying water into the autoclave after steam injection and completion of the processing cycle in order to bring about steam condensation, the amount of water sprayed into the autoclave typically being 25-50wt% of the weight of the waste at the start of processing.
  • the present system in some embodiments uses an inclined tunnel-shaped rotating-drum autoclave that has an internal Archimedes screw welded to the vessel. This is rotated in one direction during loading to facilitate the loading of the autoclave, and rotated in the other direction during operation to break up the waste and ensure that the load is evenly processed.
  • This vacuum bursts open any packaging or unopened containers and also helps to ensure that, when the steam is let into the vessel, it completely penetrates the load.
  • the chamber has reached its optimal operating conditions (160°C and several atmospheres pressure), the mixture is allowed to cook for about 40 min.
  • three types of autoclave may be supplied in pairs to allow the steam to be recycled from one autoclave to the other to save energy.
  • a relatively small autoclave has in an embodiment a seven-tonne capacity and is primarily aimed at processing food waste. 15-Tonne and 30-tonne vessels are suitable for local-authorities and large scale treatment of municipal standard waste.
  • a pair of the 30-tonne autoclaves can process around 600 tonnes a day (200,000 tonnes a year), which equates to the waste disposal needs of about 400,000 people.
  • the autoclave 10 has a cylindrical body sloping downwards as shown at about 15° and having a central cylindrical region 210 bounded at its upper and lower ends by welded-on lower and upper support rings having cylindrical side surfaces 212, 216 and lower side surfaces 214, 218.
  • the body On the further sides of the support rings the body has lower and upper tapered e.g. frustoconical or dished regions 220, 222 which are removably closed by the lower and upper doors 14, 16.
  • the autoclave is supported in a fixed attitude relative to the horizontal in a framework having first and second sides 224, 226 joined by cross-members e.g.
  • the autoclave body At its lower the autoclave body is supported for rotation in the framework by support wheels 230 carried by cross-members 228 which run on the side surface 212 of the lower support ring and by thrust rollers 232 which run on the lower side surface 214 of the lower support ring and provide a reaction for the sideways component of the load of the autoclave body and its contents (i.e. load in a direction longitudinally of the autoclave body).
  • support wheels 234 which run on the side surface 216 of the upper support ring.
  • Drive motor 238 carried by the frame is operable to rotate the autoclave body in either direction via drive chain or belt 240 and driven wheel 242.
  • the pivot mechanism for lower door 14 is as follows. At a location spaced upwards from the axis of the autoclave the support frame has fixing brackets 244, 246 for hinge pin 246 which carries hinge sleeve 248.
  • the door 14 is attached to the sleeve 248 by arm 250 and is balanced by counterweights 252, 254.
  • Fluid delivery line 256 passes along arm 250 to pressure-tight rotary pipe coupling 258 where the radially incoming steam or water is supplied to the door 14 through which it passes axially inwards and upwards into the autoclave. Flow through line 256 is controlled by valve 260, and there is an end coupling for steam and water supply pipes.
  • the upper door 16 is similarly supported by brackets 262, 264 on the frame that support hinge pin 266 and hinge sleeve 268. Similarly to the door 14, the door 16 is mounted to the hinge sleeve by arm 270 and is counter-weighted by weights 272, 274, a steam and water supply line 277 leading to control valve 276 and then to connector 278 which is visible in this view and which provides a connection to steam and water supply lines.
  • Fig. 4 is an oblique view of the autoclave from its upper end with the door 16 in its open position to reveal waste inlet 243.
  • Drive wheel 239 on the shaft of motor 238 is also apparent.
  • a safety plate 245 of metal or plastic covers the motor and drive belt 240 to reduce the risk of injury to operators of the autoclave.
  • the lower door 14 is shown in its open position for discharge of treated waste.
  • the autoclave is shown in side view in longitudinal vertical section to reveal single start or two start internal helical flights 280 thereof defining an Archimedean screw, the doors 14, 16 being shown in their open positions.
  • the amount of water added will depend on cellulosic content and should be in an amount that is effective to maintain mobility of the load during subsequent processing and to soften the lignin content of the load. It may comprise 25wt% based on the weight of the MSW, more usually about 50 wt% and if the cellulosic content is high 100% or above, the 50 wt% figure being typical.
  • the load volume at initial filling should be ⁇ 75% of the internal volume of the autoclave.
  • load cells are employed during this stage and during subsequent hot processing of the load to check for a relatively even load distribution between upper and lower parts of the autoclave, showing that the load has not remained compacted at the lower end of the autoclave.
  • steam and optionally further water are introduced through door 14 to raise the internal temperature of the autoclave e.g. to about 160° and the pressure to about 6 bar. Pressurization of the autoclave may take some minutes, substantial quantities of the introduced steam condensing in the initially cold load as indicated above to increase the water content thereof.
  • Circulation of the load through the autoclave by reverse rotation is continued, and even load distribution continues to be monitored to check that the load has not compacted and remains at the bottom of the autoclave.
  • Penetration of the steam into and through the load is gradual, and pressure is monitored at both ends of the autoclave, rise of pressure at the upper end of the autoclave to or close to the rated processing temperature ⁇ 160°C indicating that the pressurization step is complete.
  • Processing at the working temperature and pressure is then carried out for a period of time effective to break down the load and in particular any paper and cellulosic content of the load and water being added from below or above the load via door 14 and/or 16 as desired.
  • load volume material shrinks substantially during processing as plastics items are softened and board structures collapse but the mass density is increased.
  • the autoclave On completion of the processing step the autoclave is abruptly de-pressurised and water is injected through the upper door 16 and sprayed into the interior of the autoclave to collapse the steam in the load and avoid a steam plume.
  • Abrupt de- pressurising is advantageous since it disrupts any residual cell structure in the load material and makes the load contents more accessible to the microbes in the subsequent anaerobic digestion step.
  • a considerable volume of water may need to be added for this purpose, this being possible because of the load shrinkage during the thermal processing step, and the volume of added water typically being -50 wt% of the mass of the waste being treated.
  • De-pressurisation may take 10 minutes.
  • the steam from the working autoclave will, of course, be recycled to the start-up autoclave as previously described.
  • the autoclave is again subjected to vacuum treatment, this stage lasting for some minutes.
  • the direction of rotation of the autoclave is then again reversed, the lower door 14 is opened and the load is discharged, some minutes being allowed for this operation.
  • the load has now been diluted with large amounts of water so that at the end of processing the combined collapsed load and added water approximately 50% fills the autoclave, but this is not a problem because the feedstock for the subsequent AD digestion stage is desirably a dilute aqueous slurry.
  • Thermocouples and load cells for the autoclave may provide inputs for a microcontroller or computer with appropriate stored instructions e.g. to execute the following start up logic for one of a pair of autoclaves with steam recycling:
  • alternately operating autoclaves are mounted in support frames for rotation about their longitudinal axes, slope downwardly at about 15° and are provided at opposed ends with lower and upper doors.
  • the autoclaves may, for example, each process a 15 tonne load, and be of length typically 13m and diameter 3.33m.
  • Water which is preferably heated to near boiling e.g. 90°C can be pumped from a dilution tank via a lower end door of each autoclave.
  • 7.5 tonnes of water may be added at the start of the cycle through the lower door in this way.
  • Steam from an accumulator can pass through the lower end door into one or other autoclave. Typically about 3.25 tonnes of steam is injected via the bottom connection and turns into condensate.
  • either water or steam may be introduced and when required, the pressure within either autoclave can be reduced by respective vacuum pumps.
  • the autoclaves may work at 110-170°C, a temperature of 160°C and a pressure of about 6 bar being considered optimum as a feedstock to AD.
  • steam can be recycled from one of the autoclaves which is ending its processing cycle to the other autoclave which is beginning its processing cycle.
  • Recycled steam can enter through the top door.
  • condensate is re-evaporated and transferred to the other autoclave, the other autoclave then having already been loaded and evacuated by the vacuum pumps.
  • the recycled steam preheats the second autoclave before fresh steam is admitted from the steam accumulator and this minimises the quantity of fresh steam required.
  • the remaining steam in the autoclave at the end of its cycle can then be condensed by adding cold water. About 15 tonnes of water may be added at the end of the processing cycle, condensing residual steam and cooling the waste to about 70°C.
  • a waste stream from the or each autoclave passes via a conveyor to a separator e.g. a star screen for separation into an organic-rich waste stream and an mechanically separable reject stream. Recyclables pass from the separator and it is expected that about 3.5 tonnes per cycle of recyclables will be removed in this way.
  • a separator e.g. a star screen for separation into an organic-rich waste stream and an mechanically separable reject stream. Recyclables pass from the separator and it is expected that about 3.5 tonnes per cycle of recyclables will be removed in this way.
  • the organic fraction may be passed direct or with water dilution to the supercritical water oxidiser.
  • the digestible organic fraction passes to wet sorting station where it may be combined with cold water for cleaning and cooling, about 12 tonnes of water being added to cool the waste to about 50°C.
  • the waste may then be passed via a gravity conveyor to a stirred day tank which can accommodate material from several autoclave batches each amounting including condensate and added water to about 50 tonnes.
  • a stirred day tank which can accommodate material from several autoclave batches each amounting including condensate and added water to about 50 tonnes.
  • the holding tank will need to be of size about 250m 3 , and its contents may be stirred to maintain the organic materials in suspension.
  • Breakdown of the organic components in an autoclave of the general kind described above can result in a product from which an organic-rich stream can be separated, that stream being either directly subjected to supercritical water oxidation or being subjected to anaerobic digestion, resulting sludge then being subjected to supercritical water oxidation.
  • hydrolysis is the controlling step in the anaerobic digestion (AD) of organic solids.
  • AD anaerobic digestion
  • the process of hydrolysis requires weeks to complete in a traditional AD process.
  • a major disadvantage for AD of solid wastes is that the process requires large reactor capacities.
  • the majority of organic solids with an appropriate combination of contact, processing temperature and processing time can be thermally hydrolysed and liquidised.
  • the retention time for the following AD process can be significantly shortened and the digester tank size can be significantly reduced.
  • the combination of thermal and mechanical degradation induced by the autoclave has the effect of vastly increasing the amount of organic material that can be digested by AD.
  • AD ammonia toxicity to the anaerobic micro-organisms associated with treating high protein content wastes.
  • Thermal denaturation and/or hydrolysis of protein in an autoclave alleviate the inhibition of bacterial activity by ammonia build- up.
  • High protein waste includes slaughterhouse waste and animal by-product wastes as well as food waste e.g. from supermarkets and catering establishments.
  • a major problem in slaughterhouse waste is the treatment of blood, and it is believed that slaughterhouse blood waste can be treated in an autoclave of the present kind and then passed on for anaerobic fermentation without unacceptable ammonia build-up.
  • a further major weakness for AD is that the process has limited tolerance to shock loadings mainly caused by uneven qualities of feedstock. Autoclaving produces a thoroughly homogenised feedstock for the AD which significantly reduces the risks from shock loadings.
  • the bio-gas that comes off the digester is used to generate electricity.
  • the generator is only about 35% efficient, and the rest of the energy is released as heat, of which part is used to generate steam for the autoclave.
  • the resulting sludge from the digester can be burnt as bio-mass, put into a gasifier to produce 'syngas', composted or even formed into a building material.
  • EU landfill directive calls for the amount of organic waste sent to be halved by 2013, and this requirement is backed up by an escalating tax regime.
  • EU Landfill Tax is rising at a rate of £8 per tonne per year (it is currently at £40 per tonne) and is expected to reach £70 per tonne within 5 years. Including tax, the cost of disposing of waste to landfill is currently around £60 a tonne.
  • the social climate is also in favour of sustainable waste solutions; there is a general desire to show more concern for the environment, but at the same time, people do not like the idea of being fined for putting out to much rubbish or mixing up recyclable products.
  • Embodiments of the present process and apparatus not only remove the need to separate out different types of waste; they can also offer local authorities the chance to profit from their waste, rather than paying to get rid of it.
  • VFA volatile fatty acid
  • Anaerobic microorganisms used in anaerobic digestion are a mixed culture. They mainly contain three groups of bacteria: hydro lytic enzyme bacteria, acidogenic and acetogenic bacteria, and methanogenic bacteria.
  • the hydrolytic enzyme group is responsible for hydrolysing long chain organic compounds into soluble small molecular substrates which can then be converted to VFA's by the acidogenic bacteria and eventually to acetic acid by the acetogenic bacteria.
  • the methanogenic bacteria will convert acetic acid to biogas, which mainly contains methane and carbon dioxide.
  • Autoclave pre-treatment can bring about cellular disruption which can facilitate subsequent anaerobic digestion or direct supercritical water oxidation. It can hydro lyse the majority of the cellulosic material in the waste which can reduce the need for bacterial enzyme hydrolysis in a downstream anaerobic digestion process.
  • the mechanism of the metabolism of the anaerobic bacteria will be automatically emphasised on the development of methanogen. Therefore more biogas will be produced by the autoclaved materials than non-autoclaved at the same loading rates. In other words, to reach the same gas production rate, higher loading rates can be applied on the autoclaved waste than on the non-autoclaved waste. This means for treating waste streams with the same solids concentrations shorter retention time can be used on the autoclaved waste. Hence the digester volume can be reduced.
  • the organic fraction from autoclaving and screening or sludge from subsequent digestion of that fraction may be subjected to supercritical anaerobic oxidation.
  • the heat released by oxidation elevates the temperature of the water-organic-oxygen stream appreciably and it can easily reach 450°.-700°C. If the mean temperature in the oxidizer is 400°C or above then the residence time in the oxidizer can be less than 5 minutes. Since the oxidation occurs within a water phase, dirty feeds can be used without the need for off gas scrubbing. For example sulphur in the fuels can be oxidized to solid sulphate which would be readily recovered from the effluent stream from the oxidizer. Inorganics precipitate as a waste slurry, since the solubility of inorganic salts in supercritical water drops to very low levels above 450-500°C.
  • the effluent from the oxidizer can easily be designed to be above those temperatures thus causing inorganics in the stream to precipitate and be readily removed as by cyclones, settling columns or filters.
  • the water output from the system is purified of inorganic salts.
  • the heat of oxidation of the organics in the feed is recovered directly in the form of high temperature, high pressure steam.
  • a recycle reactor for carrying out processes of this type is disclosed in US 6017460 (Chematur).
  • a reactor design said to reduce clogging and corrosion is disclosed in US 2008/0073292 (Stenmark). It comprises an essentially vertical reactor section and an essentially non-vertical reactor section connected together, wherein said essentially vertical reactor section has a cross-sectional area which is substantially larger than the cross-sectional area of said essentially non-vertical reactor section, wherein: said essentially vertical reactor section has an inlet in an upper portion of said essentially vertical reactor section provided for receiving a flow comprising organic material and water; said essentially vertical reactor section is configured to receive oxidant and to oxidize organic material of said flow through supercritical water oxidation while said flow is flowed through said essentially vertical reactor section; said essentially vertical reactor section has an outlet in a lower portion of said essentially vertical reactor section provided for outputting said flow, and said essentially non- vertical reactor section is configured to receive oxidant and to efficiently oxidize organic material of said flow through supercritical water oxidation while
  • the invention may further comprise supplying an organic-rich fraction of processed waste from the autoclave to an anaerobic digester, and recovering a methane- rich gas there from.
  • the anaerobic digester advantageously operates under mesophilic or thermophilic conditions.
  • Methane-rich gas may be supplied to at least one internal combustion engine (e.g. based on reciprocating pistons or a turbine) for generation of power and exhaust gas, and generating steam for said autoclave using the exhaust gas from said internal combustion engine.
  • Recovered jacket water may be used for heating water be supplied to the autoclave and also water to be supplied to a steam generator of the autoclave or anaerobic digestion system. Recovered jacket water may also or independently be used to conduct anaerobic digestion at an elevated temperature e.g. to maintain mesophilic or thermophilic conditions
  • An anaerobic digestion plant may be operated under wet conditions, solids content being ⁇ 15% e.g. 2-15%, as a further example about 10%. It may also be operated under semi-dry conditions with solids content 15-20%) or under dry conditions with solids content 30-40%>, but these possibilities are less preferred.
  • Stirred anaerobic digestion tanks may each hold the autoclaved organic waste component for 15-30 days e.g. about 20 days, working at a content of about 10%> w/v solids content and each of liquid capacity about 2500m 3 , height 10m and diameter 21m.
  • Gas may be collected overhead and passes via a common line a to gas scrubber and then to a compressor, compressed gas at least about 0.1 barg. e.g. about 0.25 barg.
  • the process may be configured to use acidogenic and methanogenic bacteria together in a single stage as in the disclosed embodiment, or in a further embodiment the process may be operated in two stages, a first acidogenic stage and a second methanogenic stage.
  • Methane-containing gas from the digestion tanks passes to gas storage tanks which can store typically some hour or hours output, 3750m 3 at about 0.25 barg.
  • Gas from the storage tanks flows to engines where it is combusted to generate power.
  • the engines may have a rated output of e.g. 1.5MW each, discharging through their exhaust about 315GJ of heat per day with an exhaust temperature of about 500°C.
  • Exhaust gas from the engines passes to a heater coil of an accumulator required on demand to deliver 3.25 tonnes of steam. It may be sized 13m in length and 2.5m diameter, giving a capacity of about 65m 3 .
  • Liquid from the digestion tanks is pumped by a pump as jacket water for the engines, and leaves them via line 132 at 110°C.
  • a first branch line leads to heater coil of a hot well which stores water at 90°C. Water leaving the heater coil passes to a heating coil of a dryer and then returns as warm feed to the digestion tanks.
  • a second branch line passes jacket water through a heater coil a of dilution tank for maintaining the contents thereof at about 90°C.
  • Solids-rich discharge from the digestion tanks passes to a discharge tank at the same volume flow as the liquid entering the digestion tanks.
  • the discharge tank may receive about 48m 3 /hour of dilute slurry carrying about 60 tonnes per day of solids, the tank having typically a capacity of about 250m 3 .
  • Dilute slurry is pumped from the tank and is combined with flocculent from a flocculent injection tank, the combined flow then being treated as described below.

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Abstract

L'invention concerne un appareil pour le traitement des déchets ménagers ou autres, cet appareil comprenant une installation de traitement en autoclave pour traiter à la vapeur les déchets solides, ainsi qu'un réacteur d'oxydation supercritique placé en aval de l'installation de traitement en autoclave pour convertir un flux de produit en chaleur, en eau et en dioxyde de carbone. Le flux de produit peut être un flux riche en matière organique provenant de la matière autoclavée ou peut être sous la forme de boues provenant d'un digestat anaérobie du flux riche en matière organique. Dans un cas comme dans l'autre, l'élimination des boues en décharge ou par incinération est évitée.
PCT/GB2012/051335 2011-06-17 2012-06-13 Appareil et procédé pour le traitement des déchets Ceased WO2012172329A2 (fr)

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GB2546243A (en) * 2015-12-23 2017-07-19 Aerothermal Green Energy Ltd Biomass, thermal pressure hydrolysis and anaerobic digestion
CN108128999A (zh) * 2018-01-17 2018-06-08 江苏华美达生物能源有限公司 一种太湖蓝藻及污水厂污泥及餐厨垃圾协同处理方法
WO2018226414A1 (fr) * 2017-06-07 2018-12-13 Native American Construction Service, Inc. Système et procédé de génération et de stockage de gaz méthane à l'aide de sources renouvelables
CN112845096A (zh) * 2021-03-12 2021-05-28 北京都市绿源环保科技有限公司 一种生活垃圾处理装置
US11077413B2 (en) 2016-03-17 2021-08-03 Alkymar As Mixing and processing apparatus
WO2022131122A1 (fr) * 2020-12-16 2022-06-23 三菱重工環境・化学エンジニアリング株式会社 Système de traitement hydrothermique
WO2022138201A1 (fr) * 2020-12-21 2022-06-30 三菱重工環境・化学エンジニアリング株式会社 Système de traitement hydrothermal
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GB2546243A (en) * 2015-12-23 2017-07-19 Aerothermal Green Energy Ltd Biomass, thermal pressure hydrolysis and anaerobic digestion
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US11077413B2 (en) 2016-03-17 2021-08-03 Alkymar As Mixing and processing apparatus
US11230689B2 (en) 2017-06-07 2022-01-25 Native American Construction Service, Inc. System and method for generating and storing methane gas using renewable sources
WO2018226414A1 (fr) * 2017-06-07 2018-12-13 Native American Construction Service, Inc. Système et procédé de génération et de stockage de gaz méthane à l'aide de sources renouvelables
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KR20230098677A (ko) * 2020-12-16 2023-07-04 미츠비시 쥬코 칸쿄 카가쿠 엔지니어링 가부시키가이샤 수열처리 시스템
JP2022095036A (ja) * 2020-12-16 2022-06-28 三菱重工環境・化学エンジニアリング株式会社 水熱処理システム
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CN116490294A (zh) * 2020-12-21 2023-07-25 三菱重工环境·化学工程株式会社 水热处理系统
WO2022138201A1 (fr) * 2020-12-21 2022-06-30 三菱重工環境・化学エンジニアリング株式会社 Système de traitement hydrothermal
KR102859539B1 (ko) 2020-12-21 2025-09-12 미츠비시 쥬코 칸쿄 카가쿠 엔지니어링 가부시키가이샤 수열처리 시스템
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