EP1296095B1 - Anlage zur Aufbereitung von Müll durch Pyrolyse und zur Energieerzeugung durch diese Aufbereitung - Google Patents

Anlage zur Aufbereitung von Müll durch Pyrolyse und zur Energieerzeugung durch diese Aufbereitung Download PDF

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Publication number
EP1296095B1
EP1296095B1 EP02020349A EP02020349A EP1296095B1 EP 1296095 B1 EP1296095 B1 EP 1296095B1 EP 02020349 A EP02020349 A EP 02020349A EP 02020349 A EP02020349 A EP 02020349A EP 1296095 B1 EP1296095 B1 EP 1296095B1
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EP
European Patent Office
Prior art keywords
refuse
plant
reactor
steam
unit
Prior art date
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EP02020349A
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English (en)
French (fr)
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EP1296095A3 (de
EP1296095A2 (de
Inventor
Francesco Goggi
Lorenzo Goggi
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GOGGI, LORENZO
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Individual
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Priority to CY20111100185T priority Critical patent/CY1111306T1/el
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/006—General arrangement of incineration plant, e.g. flow sheets
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/50—Control or safety arrangements
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/301—Treating pyrogases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/40—Gasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/80—Shredding

Definitions

  • the present invention relates to a plant for treating solid and/or liquid refuse by pyrolysis in accordance with the introduction to the main claim.
  • the invention also relates to a method for treating refuse within the aforesaid plant, in accordance with the corresponding independent claim.
  • Refuse disposal has become a well known and increasingly urgent problem in particular in the more developed countries. Also well known is the need to recover energy from the refuse treatment and disposal process to make it increasingly attractive economically.
  • US 5980858 describes a method and apparatus for treating wastes by two-stage gasification in order to recover metals or ash content in the wastes in such a state that they can be recycled, and gases containing carbon monoxide (CO) and hydrogen gas (H 2 ) for use as synthesis gas for ammonia (NH 3 ) or production of hydrogen gas.
  • the wastes are gasified in a fluidized-bed reactor at a low temperature.
  • gaseous material and char produced in the fluidized-bed reactor are introduced into a high-temperature combustor, and gasified at a high temperature and ash content is converted into molten slag.
  • the gas is separated into H 2 and residual gas. The residual gas is then supplied to the fluidizing gas.
  • DE 4107200 and XP 000162988 both disclose a plant for treating wastes or refuses in a low temperature reactor.
  • the plant treats soil contaminated with organic or inorganic substances, contaminated wood, oil, slurry and a plastics of all types, as distinct from household refuse.
  • Contaminants include heavy metals, inorganic substances containing HC1 or CN-.
  • HC1 or CN- a separation occurs between larger, solid materials, and fine dust or gaseous material.
  • the relatively low temperature process is carried out mainly without oxygen. The process ensures that liquid fine particles and dry waste products are burnt, dust is removed from the smoke and trapped in the melted slag, heavy metal oxides are separated from the smoke for further recycling, the molten slag after cooling can be used for building material.
  • An object of the present invention is to provide a plant for treating refuse by pyrolysis which enables the refuse to be completely demolished, with the formation generally of CO 2 and H 2 , this latter being able to produce clean electrical energy which can be used to self-sustain the plant or for other ecological uses such as motor traction using hydrogen motors, and fuel cells.
  • Another object is to provide a plant of the aforesaid type which enables valuable gases, such as pure H 2 and CO 2 , to be produced and recovered for other uses external to the plant.
  • a further object is to provide a plant of acceptable maintenance and operating costs.
  • a further object is to provide a plant of the stated type which has virtually no environmental impact.
  • Another object is to provide a method for treating refuse by means of the plant of the invention, said method being of high efficiency and acceptable implementation cost.
  • the plant of the present invention is based on the high temperature pyrolysis of organic substances (substances containing essentially carbon and hydrogen) for the purpose of producing very pure H 2 gas for use as fuel in appliances such as steam-producing boilers combined with steam turbines, gas turbines combined with micro-steam turbines or fuel cells combined with micro-steam turbines; all aimed at the production of electrical energy which, besides powering energy consumers of the cycle, produce an excess to be utilized for uses external to the plant.
  • the essential concepts on which this technology is based are those of a clean and correct pyrolysis developed at high temperature and controlled with the aid of regulating and control systems preferably of microprocessor type.
  • the purpose of this is to obtain the final production of a gas of almost total molecular hydrogen composition (H 2 ) for use in fuel cells, with initial utilization in gas turbines with condensation heat exchangers to produce electrical energy and, where necessary and usable, hot water for domestic or heating purposes, with final condensation of pure water to be used within the cycle itself and of which any excess can be used either as pure (distilled) water or in mixture with potable water derived from desalination plants.
  • H 2 gas of almost total molecular hydrogen composition
  • the inert part present in the liquid or solid refuse is melted at pyrolytic temperature, vitrified by cooling in water and extracted as perfectly inert material usable for example as filling material in road covering mixtures (in view of its particle size, hardness and degree of inertness).
  • the plant of the invention comprises a reactor 1 in which pyrolysis takes place of refuse fed into said reactor 1 via a feed line 2.
  • This refuse can be solid and/or liquid.
  • This latter originates from a tank 3 connected via a pump or other feed means to a member 5 into which there converge the liquid refuse, the solid refuse from a plant portion 7 shown schematically in Figure 3 and constructionally in Figures 5 and 6 and described hereinafter, high pressure and high temperature steam metered and regulated by a measurement and control member 8V comprising a pneumatic control valve and a flowmeter (not shown), and the powder PR.
  • the liquid refuse is evaporated by the steam entering the member 5.
  • the refuse is micro-disintegrated to dimensions enabling it to be easily liquefied or pre-sublimed by the thermal energy of the steam fed into the portion 7 by metering via a pneumatic control valve and quantified by a flowmeter under the control of an operating and control unit (described hereinafter) which handles and controls the plant operation.
  • the steam is fed into the portion 7 by a feed unit 8 in determined proportions based on the type of refuse being treated.
  • gasification means the complete evaporation of the liquid refuse or the refuse previously liquefied within the plant portion 7 and the complete sublimation of the micro-disintegrated solid refuse (that which does not have a liquid phase) within the steam present in the line 2.
  • the members directly or functionally connected to the line 2 define a plant pretreatment portion for the refuse 9.
  • the refuse hence arrives at the reactor 1, at a nozzle 12 to which there also arrive an oxygen feed line 13 and a feed line 15 connected to a hydrogen tank 15A forming part of the plant or, alternatively, a tank 15B of any fuel such as liquefied gas (LPG) or methane.
  • LPG liquefied gas
  • the fuel 15B serves only for start-up until hydrogen is produced for feed into the tank 15A; the hydrogen in excess of that required for sustaining pyrolysis at the nozzle 12 of the reactor 1 (H 2 and O 2 stoichiometric combustion) feeds the electrical energy production line either comprising a boiler and steam turbine, or a gas turbine and steam micro-turbine, or fuel cells and a micro-steam turbine (not shown).
  • the reactor 1 is contained within an outer enclosure 23 provided with an interspace through which hot water circulates to recover heat from the enclosure; the reactor 1 communicates with the outer enclosure 23 through apertures 25 provided below the reactor 1 and adjusted in their degree of opening by an electromechanical device 156 controlled by a regulation and control system 147 operating on the basis of the pressure in the enclosure 23.
  • the enclosure contains heat exchangers, for example of serpentine coil type 26, arranged in several internal columns and with one column sandwiched within the enclosure 23 to produce high pressure superheated steam by the passage along its surface of hot gas from the reactor. A part of this steam is fed to the feed unit 8 and to the member 8V of Figure 3 and Figure 2 , to the jacket 10 of the line 2, and to a catalysis line 160.
  • this steam is metered and measured by the pneumatic control valve and flowmeter (regulated and controlled by the plant operating and control unit).
  • the steam is also fed to a cooling line 35A for the nozzle 12, again metered and controlled by a valve and flowmeter controlled by the control unit, and finally the excess steam is fed via a valve and flowmeter controlled by the control unit, to a heat exchanger 243 of a gas separation line 40 shown in Figure 4 .
  • the gas produced by the reactor is extracted from the enclosure 23 through a line 30 and transferred to a heat exchanger 31, for example of tube bundle type.
  • the gas undergoes violent cooling and is fed to a gas recycle plant portion 33 in which a variable-throughput motor-driven fan 34 is present to feed this pyrolysis gas to a line 35.
  • This has two branches 35A and 35B into which there are connected flowmeters 35K and metering valves 38, operated and controlled by the regulator and control unit to control the quantity of pyrolysis-produced gas to be recirculated through the reactor 1 and that to be fed to the aforesaid line 40 of Figure 4 for the gas enrichment and separation stages; for example, the valves 38 are of the pneumatic control valve type.
  • the two branches of the line 35 are connected respectively to the outside of the nozzle 12 (to create thereat a turbulence between the arriving fluids) and to the gas separation line 40 shown in Figure 4 .
  • carbon dioxide (CO 2 ) molecular hydrogen (H 2 ) and water are obtained, this latter being returned, mixed with the various wash and cooling water streams, to the plant via the said line 43.
  • Any powder material present in the fluid of line 40 is recycled and reaches the member 5 (where it is indicated by PR) and to the reactor 1 where it is inerted and vitrified.
  • the refuse pretreatment portion 9 will now be analyzed in greater detail. As stated, this latter comprises the portion 7 where the solid refuse is micro-disintegrated and mixed with the high pressure, high temperature steam from the serpentine coils 26. With reference to Figures 3 , 5 and 6 , the portion 7 is shown comprising a container 70 in which the solid refuse is collected. This latter is fed into a hopper 71 in which a mixer 72 is positioned, driven by its own electric motor 73.
  • the hopper lowerly presents a metering screw 74 (shown schematically in Figure 3 as coaxial with the hopper, but in reality positioned as shown in Figure 5 ) terminating with a frusto-conical end 75 by means of which the refuse R is pressed and directed towards a first disintegrating unit 76 provided with a disintegrating member 77 (for example defined by moving disintegration blades) and a conveying member 78 defined for example by a screw.
  • the member 78 caries the refuse (via a frusto-conical part 76A), subjected to first disintegration, towards a second disintegrating unit 80 provided with a disintegrating member 81 and a conveying member 82 totally similar to the said members 77 and 78.
  • the conveying member 82 carries the now finely disintegrated (or rather micro-disintegrated) refuse towards a dispensing zone 84 of the second disintegrating unit where a container 85 is present having its longitudinal axis W perpendicular to the axis T of the unit 80 and acting as an "overflow" member or dispensing member for the micro-disintegrated refuse.
  • This container comprises a piston 87 positioned above its contents and pressed onto the refuse with a pressure obtained by feeding air above the piston via a suitable conduit 80.
  • An adjustable bleed member 91 is positioned at the closed top 92 of the container 85 (where the conduit 90 is connected) and enables the pressure in the container to be regulated.
  • the piston 87 is associated with a rod 95 emerging from the top 92 and cooperating with a proximity sensor 96 carried by a support 97 (position measurer or encoder) fixed to said top.
  • a proximity sensor 96 carried by a support 97 (position measurer or encoder) fixed to said top.
  • this sensor On the basis of the relative position of the rod 95, this sensor generates a proximity signal directed towards a control unit 100 (data processing unit for the management and control of all the processes described in the present text), preferably a microprocessor member and a programmed logic interface, which controls the entire plant and operates each moving member (motor, valve, flow meters, or other) present therein.
  • the unit 100 controls the speed of the geared motors 73 and of the motors 74A of the screw 74, 78A of the member 78 and 82A of the member 82 of the plant portion 7. In this manner the quantity of refuse fed to the reactor 1 is controlled to prevent an excess of refuse in this latter.
  • the dispensing zone 84 is connected, by a conduit 101 leaving a frusto-conical part 80A, to a further conveying member 102 inserted into a transfer unit 103 (provided with its own geared motor 102A also controlled by the unit 100) which is connected to the refuse reception unit 5 to which it transfers the micro-disintegrated refuse liquefied or pre-sublimed by the steam fed into the disintegrating unit 76.
  • vacuum (indicated by X in Figure 3 ) is preferably applied to the first disintegrating unit 76.
  • the refuse in the section 7 is also heated by steam flowing through a double wall positioned about the screws 78, 82, 102, and by the hot water within the interspace of the screw 74.
  • the liquid refuse also reaches the member 5 through a conduit 110 into which the pump 4, a normally closed pneumatic safety valve 111, a non-return valve 112 and a flowmeter 111k are connected, this latter, by means of the unit 100, controlling the throughput of the pump 4 under the control of an electronic inverter (not shown).
  • Another unidirectional valve 113 is also present in the line 2 to prevent refuse returning from the reactor 1 to the member 5 because of any excess pressure present in said reactor.
  • a normally closed spring-operated safety valve 114 for any overpressure
  • a metering valve 115 operated and controlled by the unit 100
  • temperature and pressure measuring devices for the fluid in the line 2, indicated by 118 and 119 respectively.
  • the line 2 also presents a jacket 10 through which steam circulates originating from the serpentine coil 26. This steam raises the temperature of the fluid (steam with evaporated liquid refuse and micro-disintegrated solid refuse) flowing through the line 2 towards the reactor 1.
  • this line is defined by several segments joined together by flanges F, by-pass lines 120 for the jacket 10 are present around these flanges.
  • Figure 7 also shows a conduit 8Z connected to the member 8V to feed steam into the line 2 (fully described hereinbefore) and conduits 122 for feeding steam into the jacket 10.
  • the line 2 is connected to a multiple pipe 125 presenting a central section S1 and concentric annular sections S2, S3 and S4, visible in Figures 7 and 8 . These sections are connected respectively to the line 2, to the oxygen feed line 13, to the hydrogen or fuel feed line 15, to a line 201 carrying cooling steam for the nozzle 12 and to the branch 35A of the line 35 which carries recirculation gas to the reactor 1.
  • This gas advantageously creates turbulence between the other fluids leaving the nozzle 12 to hence enable complete pyrolysis of the refuse fed into the reactor.
  • an annular chamber 127 is present through which the gas produced by the said pyrolysis recirculates.
  • apertures 130 are preferably inclined and made with interchangeable nozzles having different diameter holes such as to cause the oxygen to emerge at sonic velocity to create turbulence within the fluid containing the pre-gasified refuse; those apertures 128, carrying a part of the O 2 , the fuel and the cooling steam to the nozzle 12, are formed, for example, as cuts having right or left helixes such as to widen the flame and create maximum turbulence within the inner part of the nozzle 12 where pyrolysis at very temperature occurs.
  • the (main) section S1 through which the fluid containing the "gasified" refuse arrives can be closed by a closure member 131 movable within that section.
  • Said member 131 is carried by an end 132A of a rod 132, the other end 132B of which is subjected to an actuator member 133 (pneumatic, mechanical or electrical) in order to be able to move in a guided manner within the section S1.
  • That end 132A carries a disc 134 on which there acts a spring 135 inserted into a chamber 136 within which the disc moves, between this latter and a chamber end face 136A through which the rod 132 passes.
  • the closure member can cooperate with a projecting edge 200 formed in the interior of the section S1.
  • the nozzle 12 presents fins 12A which separate it from the wall 1A of the reactor 1 and enable the gas produced by the refuse pyrolysis to be recirculated.
  • the various sections S2, S3 and S4 are connected to the respective lines 13, 15 and 201 as shown in Figure 7 .
  • the lines 13 and 15 are conceptually similar: both are connected, for example, to gas tanks (respectively oxygen (gaseous or liquid) 13K and hydrogen 15K or methane gas or liquefied propane gas 15B), and present a plurality of normally closed valves 13V and 15V, non-return valves 13N and 15N, metering valves 13D and 15D and mass flowmeters 13M and 15M.
  • gas tanks gas tanks
  • oxygen gaseous or liquid
  • hydrogen 15K gas or liquid
  • metering valves 13D and 15D mass flowmeters
  • mass flowmeters 13M and 15M mass flowmeters
  • the pure oxygen is obtained from a self-contained unit fed with electrical energy produced by the plant.
  • valve members are present in the branches 35A and 35B of the line 35, and a control valve 139 in a bypass line 137 in the plant portion 33 which connects together the entry conduit 137A to the fan 34 and the exit conduit 137B therefrom.
  • This conduit 137B is connected to the line 35, at its connection point there being a pressure sensor 140.
  • Similar pressure sensors are present in the lower part of the reactor 1 (sensor 141), in the upper part of the enclosure 23 (sensor 142) and in the lower part thereof (sensor 143).
  • Temperature sensors are also present, specifically 145 and 146 positioned respectively in the upper part of the enclosure 23 and of the reactor 1, 147 and 148 positioned in the lower part of this latter and of the enclosure 23, and 146C for measuring the temperature of the enclosure itself.
  • Other temperature sensors 150 and 151 are positioned at the two ends of the heat exchanger 31.
  • the level indicator 152 is connected to the lower part 18 of the reactor 1, to which there is also connected the mechanical linear control actuator 156 which regulates the degree of opening of the passages 25 (controlled by the unit 100).
  • the pyrolysis gas leaving the enclosure 23 passes through the line 30.
  • catalysis steam from a line 160 (suitably controlled and metered by a control valve and flowmeter controlled by the unit 100), plus the steam from the serpentine coil line 26; hot water passes through an interspace (not shown) of the enclosure 23, present along the wall of the reactor 1, in order to cool this wall.
  • the line 40 comprises a plurality of catalytic converters 240 (two in Figure 4 ) connected in series. Their function is to oxidize carbon monoxide to carbon dioxide (CO ⁇ CO 2 ) present in the gas or fluid originating from the reactor 1, so increasing the temperature of this latter.
  • a filtration unit 241 is present in series with the converters 240, to filter off and retain powder material present in the fluid originating from the reactor; this unit 241 is connected to a recirculation member 242 for the retained powder, and 242A for the metered powder for the pyrolysis, which are returned to the cycle at the member 5 (and indicated by PR in Figure 2 ).
  • the unit 241 is followed by a heat exchanger 243 and then a quenching unit 244 comprising a scrubbing, purification and cooling unit 245 for the pyrolysis gas and a droplet separation unit 246 for recovering the water present in the fluid originating from the reactor. This water is then returned to the reactor 1 via the line 43.
  • the line 40 further comprises, downstream of the unit 244, a concentrator 247 comprising, in the example of Figure 4 , a unit 248 for enriching the CO 2 -H 2 mixture still present in the fluid originating from the unit 244. Carbon dioxide is also absorbed in the unit 248 by a suitable known solvent. Downstream of the unit 248 there is a unit 250 for scrubbing the enriched H 2 gas and removing the residues of the solvent used in the unit 248. The scrubbing water is recycled to the line 43.
  • a concentrator 247 comprising, in the example of Figure 4 , a unit 248 for enriching the CO 2 -H 2 mixture still present in the fluid originating from the unit 244. Carbon dioxide is also absorbed in the unit 248 by a suitable known solvent. Downstream of the unit 248 there is a unit 250 for scrubbing the enriched H 2 gas and removing the residues of the solvent used in the unit 248. The scrubbing water is recycled to the line 43.
  • Gaseous H 2 can hence be obtained from the unit 250 for compression by a compressor 250A into the tank 15A, from which there flows that part fed via the line 15 to pyrolysis and the excess part utilized for various uses, for example for the fuel cells to produce electrical energy for operating the plant, any excess being sold.
  • the unit 248 is finally connected to a solvent storage tank 248S via the line 254A.
  • the solvent is recirculated to the unit 248 by a pump or other device 254P via the line 254B, the CO 2 -laden solvent returning to the tank 248S via a line 254A; a pump 253P withdraws the CO 2 -laden solvent from the tank 248S and feeds it to a stripping column 251 via the line 253A where countercurrent air from a fan 255 passing through a line 256 removes the CO 2 from the solvent and discharges it with the air through the vent 257; the purified solvent returns to the tank 248S via the line 253B.
  • the aforedescribed concentrator 247 can alternatively comprise a CO 2 -H 2 mixture enrichment unit with mixture compression for separation through a membrane, a unit for freezing the CO 2 and separating it from the residual H 2 , then loading it into cylinders for industrial use, and a unit for scrubbing the enriched H 2 gas and removing miscellaneous residues and recycling the water to water make-up, to give virtually pure H 2 .
  • the refuse a) provides the fuel (together with the line 15), the oxygen b) is the combustion support and the water c) is the oxidizing agent.
  • the plant provides:
  • the plant In its primary function, the plant enables solid and liquid refuse of organic origin (almost the whole of existing refuse) to be eliminated (without pollution) while at the same time enabling clean electrical energy to be produced from waste materials. Refuse is eliminated without pollution because the residues are electrical energy, pure water without salts, and vitrified inerts, only carbon dioxide being discharged to atmosphere; in the highest performance case the CO 2 is also recovered, for use in the plastic industries, welding etc.
  • the final result in the highest performance case is therefore to transform what is merely refuse for disposal (more or less bulky and noxious refuse) into electrical energy as a clean and renewable source, usable inerts (for example for road coverings) and CO 2 for industrial uses.
  • the plant of the invention is summarily described hereinafter in terms of its innovative components.
  • the plant as described hence comprises:

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Coke Industry (AREA)

Claims (26)

  1. Anlage zum Behandeln von festem und/oder flüssigem Abfall, die eine Umgebung oder eine Reaktor (1), in der/dem der Abfall (R) einer Pyrolysebehandlung unterzogen wird, umfasst, wobei der Abfall (R) dem Reaktor (1) durch Zuführungsmittel (2) zugeführt wird; Mittel (19, 40) angeordnet sind, um die festen, flüssigen und gasförmigen Produkte, die aus der Abfallpyrolysebehandlung stammen, zum gewinnen und/oder zu behandeln, und mit dem Reaktor (1) verbunden sind; das Zuführungsmittel (2) Mikrozerkleinerungsmittel (76, 80) und Vorvergasungsmittel (2, 5) zum Überführen des flüssigen Abfalls in die gasförmige Phase und des festen Abfalls in die Dampf- oder gasförmige Phase vor ihrer Einleitung in den Reaktor (1) umfasst, damit die gesamte Masse an Abfall geeignet ist, die thermische Behandlung mit ihrer anschließenden vollständige Demolition durchzumachen; wobei die Mikrozerkleinerungsmittel und Vorvergasungsmittel ein Aufnahmeelement (5) umfassen, das angeordnet ist, um den flüssigen Abfall aus einer Beschickungsleitung (110) aufzunehmen und den festen Abfall, der in einem Anlagenteil (7), der Mikrozerkleinerungsmittel (76, 80) aufweist, bereits zerkleinert wurde, aufzunehmen; wobei das Aufnahmeelement auch Dampf mit hohem Druck und hoher Temperatur aufnimmt; der Abfall aus dem Element (5) zu dem Reaktor (1) befördert wird; das Zuführungsmittel eine Leitung (2), verbunden mit dem Aufnahmeelement (5) für den vorvergasten und mikrozerkleinerten Abfall, zum Befördern des vorvergasten Abfalls zu dem Reaktor (1) umfasst; die Zuführungsleitung (2) mit einer Hochdruck- und Hochtemperatur-Dampfzuführung (8V) zum Vergasen des Eingangsabfalls verbunden ist, dadurch, gekennzeichnet, dass die Leitung (2) einen perimetrischen Zwischenraum oder einen Mantel (10) hat, durch welchen Dampf im Gegenstrom mit hohem Druck und hoher Temperatur zirkuliert, um die Vergasung des Abfalls zu verstärken.
  2. Anlage, wie sie in Anspruch 1 beansprucht ist, dadurch gekennzeichnet, dass die Mikroerkleinerungsmittel wenigstens eine Zerkleinerungseinheit (76, 80) umfasst, die ein Zerkleinerungselement (77, 81), welches den Abfall gemischt mit Dampf, welcher durch eine geeignete Einheit (8) zugeführt wird, aufnimmt", ein Beschickungselement (74, 78) und ein Transportelement (78, 82) aufweist, welches den mikrozerkleinerten Abfall zu einem Ausgang transferiert, der in einem sich verengenden Teil (76A, 80A) angeordnet ist; wobei die Zerkleinerungseinheit (76, 80) Dampf mit hohem Druck und hoher Temperatur aufnimmt; wobei ein Dämpfzuführungselement (8) mit der Zerkleinerungseinheit (76, 80) verbunden ist.
  3. Anlage nach Anspruch 2, dadurch gekennzeichnet, dass Mittel (8, 8V) zum Abmessen das (Wasser-) Dampfs, der in die Zerkleinerungseinheit (76, 80) geleitet wird und in die Zuführungsleitung (2) und den perimetrischen Zwischenraum oder den Mantel (10) der Leitung geleitet wird, angeordnet sind.
  4. Anlage nach Anspruch dadurch gekennzeichnet, dass die Zuführungbleitung (2) in ein Mehrfachrohr (125) führt, das verschiedene Abschnitte (S1, S2, S3, S4) aufweist, die in eine Düse (12) führten und mit der Leitung (2), mit einer Brennstoffzuführungsleitung (15), mit einer Verbrennungsträger-Zuführungsleitung (13), mit einer Hochdruck- und Hochtemperatur-Dampfzuführungsleiturig (201) zum Kühlen der Düse (12) bzw. mit einer Leitung (35A), welche das pyrolytische Gas unter Erzeugung von Turbulenz in den Fluiden, die die Düse (12) verlassen, umwälzt, verbunden sind.
  5. Anlage nach Anspruch 4, dadurch gekennzeichnet, dass ein kontrolliertes schließelement (131) in dem Abschnitt (S1) des Mehrfachrohrs (125), der mit der Abfallzuführungsleitung (2) verbunden ist, vorhanden ist, um den Abfallstrom zu dem Reaktor (1) zu regulieren, bis es diesen Strom unterbricht, wenn es mit dem Sitz (200) zusammenwirkt, der an der Wand (125A), die diesen Abschnitt (S1) definiert, angeordnet ist.
  6. Anlage, wie sie in Anspruch 4 definiert ist, dadurch gekennzeichnen, dass der gepulverte Abfall, der aus anderen Teilen der Anlage zurückgeführt wird, die Düse (12) auch aus anderen Teilen (242, 242D) der Anlage über die Leitung (35A) erreicht.
  7. Anlage, wie sie in Anspruch 4 beansprucht ist, dadurch gekennzeichnet, dass die Düse (12) äußere Rippen (12A) aufweist.
  8. Anlage, wie sie in Anspruch 4 beansprucht ist, dadurch gekennzeichnet, dass die Verbrennungsträger-Zuführungsleitung (13) mit einer Sauerstoffquelle (13K) verbunden ist.
  9. Anlage, wie sie in Anspruch 4 beansprucht ist, dadurch gekennzeichnet, dass, die Brennstoffzufuhrungsleitung (15) mit einem Wasserstofftank (15A) oder einem Tank für Brennstoffgas (Methan oder LPG) (15B) verbunden ist.
  10. Anlage, wie sie in Anspruch 4 beansprucht ist, dadurch gekennzeichnet, dass die Brennstoffzuführungs- und Verbrennungsträger-Leitungen (13, 15), die, mit dem Mehrfachrohr (125) verbunden sind. Dosierventile (13D, 15D) und andere Ventilelemente (13V, 15V), die durch die, Anlagen-Steuerungsmittel (100) gesteuert werden, umfassen, wobei diese letztgenannten auch mit Druck- und Temperatursensoren (119, 118), mit Ventilelementen (114, 115) und mit einem Durchflussmessgerät (111K), positioniert in oder verbunden mit der Abfallzuführüngsleitung (2), verbunden sind.
  11. Anlage, wie sie in Anspruch 2 beansprucht ist, dadurch gekennzeichnet, dass das Zerkleinerungselement (77, 78) eine Vielzahl von beweglichen Zerkleinerungsmessern umfasst.
  12. Anlage, wie sie in den Ansprüchen 1 und 2 beansprucht ist, dadurch gekennzeichnet, dass sie wenigstens zwei Zerkleinerungseinheiten (76, 80), die in Kaskade zusammengeschaltet sind, umfasst, wobei die erste (76) den festen Abfall, der zu zerkleiner ist, durch einen Schneckenförderer (74), an dem der Abfall aus einem Trichter (70), der vorzugsweise mit einem Mischer (72) ausgestattet ist, ankommt, aufnimmt, wobei die zweite Zerkleinerungseinheit (80) den mikrozerkleinerten Abfall zu dem Aufnahmeelement (5) führe.
  13. Anlage, wie sie in Anspruch 12 beansprucht ist, dadurch gekennzeichnet, dass zwischen dem Aufnahmeelement (5) und der zweiten Zerkleinerungseinheit (80) eine Transfereinheit (103) vorhanden ist, wobei diese Einheiten zueinander senkrecht sind, die zweite Zerkleinerungseinheit (80) zu der ersten Einheit (76) ebenfalls senkrecht positioniert ist.
  14. Anlage, wie sie in Anspruch 2 beansprucht ist, dadurch gekennzeichnet, dass die Zerkleinerungseinheit (80) Regulatormittel (85, 87, 95, 96) umfasst, die den Strom von mikrozerkleinertem Abfall zu dem Aufnahmeelement (5) regulieren.
  15. Anlage, wie sie in Anspruch 2 beansprucht ist, dadurch gekennzeichnet, dass die Regulatormittel einen Behälter (85), der mit seiner Längsachse (W) senkrecht zu der Längsachse (T) der Zerkleinerungseinheit (80) positioniert ist, Mittel (87, 95, 96), die in dem Behälter angeordnet sind, um die Abfallmenge abzumessen, welche in den Behälter eingedrungen ist und in diesem gesammelt wurde, und zwar vor seinem Austritt aus dem zulaufenden Teil (80A) der Zerkleinerungseinheit (80) in Richtung des Aufnahmeelements (5), umfasst, wobei die Abmessmittel (87, 95, 96) mit Anlagensteuerungsmittel (100) verbunden sind, welche auf der Basis der Abfallmenge, die in dem Behälter (85) vorlegt, die Strömungsgeschwindigkeit des Abfalls zu dem Reaktor (1) steuern und jedes gesteuerte bewegliche Element, das in der Anlage vorhanden ist, steuern, um zu ermöglichen, dass die Pyrolysebehandlung an dem Abfall vorgenommen wird.
  16. Anlage, wie sie in Anspruch 15 beansprucht ist, dadurch gekennzeichnet, dass die Abmessmittel ein Kolben (87) sind, der innerhalb des Behälters (85) unter der Wirkung des Abfalls (R) und gegen eine Widerstandskraft beweglich ist, wobei der Kolben (87) mit einer Stange (95) verbunden ist, die vor einem Näherungssensor (96) bewegbar ist, welcher mit den Anlagensteuerungsmitteln (100) verbunden ist.
  17. Anlage, wie sie in Anspruch 16 beansprucht ist, dadurch gekennzeichnet, dass die Widerstandskraft ein Fluid unter Druck, vorzugsweise Luft, ist, wobei der Druck einstellbar ist.
  18. Anlage, wie sie in Anspruch 16 beansprucht ist, dadurch gekennzeichnet, dass die Anlagensteuerungsmittel (100) eine Mikroprozessoreinheit umfassen.
  19. Anlage, wie sie in Anspruch 2 beansprucht ist, dadurch gekennzeichnet, dass in der Zerkleinerungseinheit (76, 80) Vakuum erzeugt wird.
  20. Anlage, wie sie in Anspruch 1 beansprucht ist, dadurch gekennzeichnet, dass der Reaktor (1) in einem Behälter oder einem Gehäuse (23) lokalisiert ist, in dem sich Wärmetauscher (26) befinden, um Dampf mit hoher Temperatur und hohem Druck zu erzeugen, der auch in dem Zuführungsmittel (2) zu verwenden, ist, wobei die Wärmetauscher durch die gasförmigen Produkte, die aus der Abfallpyrolyse stammen, umgeben sind.
  21. Anlage, wie sie in Anspruch 1 beansprucht ist, dadurch gekennzeichnet, dass sie ein Gaskühlungselement (31) und Steuerungsventile (38, 139) zum Abtrennen des Gases, das durch die Abfallpyrolysereaktion, im Reaktor erhalten wird, umfasst, wobei das Element mit einem Anlagenteil (33), der zum Umwälzen der Fluide durch die Anlage angeordnet ist, verbunden ist, wobei an dem genannten Teil eine Leitung (35), die zwei Verzweigungen (35A, 35B) umfasst, angeschlossen ist, wobei die erste Verzweigung (35A) zu dem Reaktor (1) führt und eine zweite Verzweigung (35B) zu einer Trennungsleitung (40) für das produzierte Reaktionsgas führt.
  22. Anlage, wie sie in Anspruch 21 beansprucht ist, dadurch gekennzeichnet, dass die Trennungsleitung (40) katalytische Wandler (240), eine Filtrationseinheit (241), um Pulver, das in dem Übertragungsfluid vorhanden ist, zu gewinnen, eine Abschreckungseinheit (244) und eine Konzentrierungsvorrichtung (247) umfasst, um zu ermöglichen, dass in dem Fluid vorhandenes CO2 und H2 abgetrennt und möglicherweise wiedergewonnen werden.
  23. Verfahren zur Behandlung von Abfall durch Pyrolyse in einer Anlage nach einem oder mehreren der vorangehenden Ansprüche, wobei der Abfall mikrozerkleinert wird, bevor er zu einem Reaktor (1) geführt wird, in dem die Pyrolyse stattfindet, wobei die mikrozerkleinerten Abfälle vorvergast werden, bevor sie zu dem Reaktor (1) geführt werden, d.h. der flüssige Teil des Abfalls wird in die gasförmige Phase übergeführt und dem mikrözerkleinerten festen Teil wird Dampf hoher Temperatur und hohem Druck zugeführt, um ihn zu verflüssigen und dann zu verdampfen oder zu sublimieren, bevor der Abfall in den Reaktor (1) eintritt, wobei die mikrozerkleinerten und verdampften flüssigen Abfälle zu einer Zuführungsleitung (2) geführt werden, in welcher der Dampf mit hohem Druck und hoher Temperatur zirkuliert, wobei der Dampf die Temperatur des mikrozerkleinerten feine Abfalls und des verdampften flüssigen Abfalls erhöht, so dass der Abfall vollständig verglast wird, bevor er den Reaktor erreicht, dadurch gekennzeichnet, dass ein weiteres Erhitzen des Abfalls erreichte wird, indem die Außenseite der Zuführungsleitung (2) erhitzt wird, wenn der Abfall bewegt wird, und zwar durch (Wasser-) Dampf mit hohem Druck und höher Temperatur im Gegenstrom, wobei der letztgenannte in den perimetrischen Zwischenraum oder den Mantel (10) der Zuführungsleitung (2) strömt.
  24. Verfahren nach Anspruch 23, dadurch gekennzeichnet, dass der Dampf, der in die Zuführungsleitung (2) und in den perimetrischen Zwischenraum oder den Mantel (10) strömt, aus dem Reaktor (1) kommt.
  25. Verfahren nach Anspruch 23, dadurch gekennzeichnet, dass der Dampf auch in den Abfall während seiner Mikrozerkleinerund eingeleitet wird.
  26. Verfahren, wie es in Anspruch 25 beansprucht list, dadurch gekennzeichnet, dass der Dampf, der zu dem Abfall, der Zuführungsleitung (2) und dem Mantel (10) der letztgenannten geleitet wird, dosiert und abgemessen wird.
EP02020349A 2001-09-24 2002-09-12 Anlage zur Aufbereitung von Müll durch Pyrolyse und zur Energieerzeugung durch diese Aufbereitung Expired - Lifetime EP1296095B1 (de)

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ES2355710T3 (es) 2011-03-30
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ATE489584T1 (de) 2010-12-15
PT1296095E (pt) 2011-02-08
CY1111306T1 (el) 2015-08-05
DK1296095T3 (da) 2011-02-28
EP1296095A2 (de) 2003-03-26
DE60238377D1 (de) 2011-01-05
ITMI20011981A0 (it) 2001-09-24

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