EP1377649B1 - Installation et procede pour produire de l'energie par pyrolyse - Google Patents

Installation et procede pour produire de l'energie par pyrolyse Download PDF

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Publication number
EP1377649B1
EP1377649B1 EP02708128A EP02708128A EP1377649B1 EP 1377649 B1 EP1377649 B1 EP 1377649B1 EP 02708128 A EP02708128 A EP 02708128A EP 02708128 A EP02708128 A EP 02708128A EP 1377649 B1 EP1377649 B1 EP 1377649B1
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EP
European Patent Office
Prior art keywords
gas
installation
pyrolysis
combustion
pyrolysis zone
Prior art date
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.)
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EP02708128A
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German (de)
English (en)
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EP1377649A1 (fr
Inventor
John E. E. Sharpe
Jack R. Metz
Reinhard W. Serchinger
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Gautschi Ulrich
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Gautschi Ulrich
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Classifications

    • 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
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F23G5/0273—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage using indirect heating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/32—Other processes in ovens with mechanical conveying means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/32—Other processes in ovens with mechanical conveying means
    • C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
    • 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
    • C10J3/007—Screw type gasifiers
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/62—Processes with separate withdrawal of the distillation products
    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/30—Cyclonic combustion furnace
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/80—Furnaces with other means for moving the waste through the combustion zone
    • F23G2203/801—Furnaces with other means for moving the waste through the combustion zone using conveyors
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying

Definitions

  • the invention relates to a plant and a method for energy production, as described in the preambles of claims 1 and 12.
  • pyrolytic processes can be used to energize waste or residual materials.
  • residues such as municipal and industrial waste, recycling sorting waste, waste and residual wood, sewage sludge, animal meal, etc. in question.
  • the pyrolytic processes are based on degassing of the carbonaceous residues provided as fuels under high temperatures and essentially with the exclusion of oxygen.
  • the energy contained in the resulting gases can be determined, for example, by combustion, i. Oxidation, which convert gases into thermal energy.
  • Thermal energy is relatively easy to use, for example, to generate heat, cold or electricity.
  • Carbo-V process Another, under the name Carbo-V process, become known method provides to decompose mainly wood-containing residues in a first reactor by partial oxidation into their volatile and solid constituents.
  • the solid constituents predominantly carbonaceous coke, are ground.
  • the resulting, very tar-containing gas is post-oxidized in the upper part of a combustion chamber, while in the lower part of the combustion chamber, the coke dust is converted into gasification gas.
  • This gas is cooled and purified several times along with the first stage synthesis gas.
  • the purified gas is then provided for generating useful energy.
  • the complex wet cleaning can be seen as a disadvantage.
  • the system required for this process must also be relatively large and complex for economical operation. Moreover, this process is essentially intended only for the energy recovery of wood.
  • a plant according to the preamble of claim 1 in which the gases are first fed to an outer surface of the pyrolysis tube in order then to pass via a conduit far from the pyrolysis tube to a heat exchanger. Only the heat exchanger performs a conversion into a useful energy form, namely water vapor.
  • WO-A-97/15641 also discloses a plant in which the hot combustion gases produced by degasification and pyrolysis can be used conventionally for steam generation.
  • the invention is therefore an object of the invention to provide a generic system and a method that allow a good balance of energy even with small plant size.
  • This object is achieved in a system of the type mentioned in the present invention that the combusting gas and / or the resulting flue gas by means of a portion of the conduit means, and with respect to their flow direction, at the same time with the passage to the pyrolysis substantially also at least one Section of a heat exchanger are passed, wherein the heat exchanger receives in a first region thermal energy of the gases and emits them in a second area to a medium of the heat utilization device.
  • the object is also achieved by a method as described in claim 12.
  • a portion of a stream of hot combustion or flue gases produced during combustion is not supplied, as in the prior art, exclusively to successive different recycling purposes, but preferably already during combustion and immediately thereafter substantially simultaneously is used both for heating the pyrolysis zone as well as for the release of thermal energy to a heat exchanger.
  • predefined physical conditions are created. This is intended to keep the temperature prevailing in the pyrolysis zone at a value which is favorable for the pyrolysis, within a certain temperature range. This temperature range may be, for example, from 850 ° C to 950 ° C.
  • This temperature range may be, for example, from 850 ° C to 950 ° C.
  • the temperature of the combustion gases during combustion or immediately thereafter in a range of about 1000 ° C to 1200 ° C, preferably from 1050 ° C to 1150 ° C and more preferably about 1100 ° C, is located on the one hand to have good results in the pyrolysis process and on the other hand a sufficient amount of energy for the generation of useful energy available.
  • This temperature range has also proved to be particularly advantageous because at On the one hand certainly no recombination of the combustion or flue gases to dioxins and furans takes place at these temperatures.
  • the temperatures are high enough to lead the flue gases over a longer distance in the conduit means before they cool to temperatures at which such recombinations would be to be feared in significant quantities.
  • the pyrolysis zone should adjoin the first boundary surface and the second boundary surface should be part of the heat exchanger.
  • the pyrolysis zone has at least one substantially elongated tube which is surrounded by an annular conduit means, the longitudinal extension of which can extend substantially parallel to the longitudinal extent of the pyrolysis tube.
  • an (outer) wall of the pyrolysis tube can also function as an inner wall of the conduit means, whereby a particularly good heat transfer into the pyrolysis zone is possible.
  • An outer wall of the conduit means may be formed as a heat exchanger, whereby also a particularly good heat transfer to the heat exchange medium with very low heat losses is possible. This also makes it possible to realize an inventive system with a particularly low design effort.
  • the pyrolysis tube and the conduit means are each circular in cross-section with the conduit means concentrically surrounding the pyrolysis tube.
  • a plurality of pyrolysis tubes can also be arranged in an annular cross-sectional conduit means, wherein the cross-sectional shapes of the conduit means and the pyrolysis tubes can be optimized with regard to good heat transfer.
  • the cross-sectional shapes of the tubes can be chosen almost arbitrarily.
  • the heat exchanger discharges the energy to a boiler in which water vapor is generated, which in turn can be used to produce a usable form of energy, such as heat, cold or electricity.
  • a boiler in which water vapor is generated
  • the conduit means and thus also the heat exchanger are arranged over at least a portion of the conduit means completely within the kettle. This may have the consequence that the pyrolysis zone, at least over a section along a conveying path of the fuel through the pyrolysis zone, is also located completely within the heat exchanger and thus also the heat exchange medium.
  • system according to the invention can be provided with a control circuit in which one or more parameters of the water vapor emerging from the boiler are measured. These measurement results can be used to control the feed rate of fuel into the pyrolysis tube so that the values of the vapor parameters are set to be substantially constant.
  • these systems should have a modular construction.
  • the systems can be provided with predefined interfaces to which system components can be interconnected by preferably detachable connections. This also makes it possible to adapt existing systems quickly and with little effort to changing conditions.
  • Fig. 1 an inventive plant for the conversion of residues is shown in energy.
  • the plant has an input point 1, can be given in the residual material 2 in an intermediate silo 3 of the plant.
  • the intermediate silo 3 is used for intermediate storage of residues 2 before they are fed to the recovery described in more detail below.
  • a arranged in a downpipe conveyor 4 follows.
  • the feed wheel 4 and / or stored in the silo 3 residues 2 conclude on this side of the plant the latter substantially airtight.
  • the downcomer opens in the region of one end of a horizontally oriented tube 5 in the latter.
  • a rotatably driven screw conveyor 6 is arranged, which promotes the residues 2 in the region of the other end of the tube 5.
  • an opening is present in the tube 5, through which the residues pass through a further downpipe 7 into a region of a front end of a pyrolysis zone designed as a pyrolysis tube 8.
  • a rotatably drivable screw conveyor 9 is arranged, with which the residues 2 are conveyed from an inlet opening 8a to a provided at the other end of the pyrolysis tube lower outlet opening 8b.
  • the pyrolysis tube 8 is sealed against an air inlet.
  • the latter end of the pyrolysis tube opens into a silo-like container 10, in which below the pyrolysis tube 8 a gasification chamber 11 and above a gas mixing chamber 12 is formed.
  • the gasification chamber 11 also belongs to a reaction part of the plant.
  • the residual substances 2, which have passed through the pyrolysis tube 8 and an essentially anaerobic pyrolysis, thus fall downwards into the gasification chamber 11 provided with a lower funnel-shaped end due to gravity through the outlet opening 8b of the pyrolysis tube 8.
  • the funnel-shaped end finally ends in another Pipe 14 with screw conveyor 15 through which the end products of the gasification process, essentially ash or slag, in a predetermined amount and time can be removed from the plant.
  • the gasification chamber 11 is connected to the outlet opening 8b of the pyrolysis tube 8 and bypass channels arranged on both sides thereof around the pyrolysis tube with the gas mixing chamber 12.
  • the resulting in the pyrolysis tube gases such as methane and carbon monoxide, thus can escape through the outlet opening 8b upwards also in the gas mixing chamber 12.
  • the gas mixing chamber is connected to a burner having a ring burner 21.
  • the combustion device 21 is in this case arranged over the full circumference of the pyrolysis tube 8 around the latter.
  • the in Fig. 2 in a first embodiment in a cross-sectional view shown in more detail laterally arranged next to the gas mixing chamber annular burner uniformly distributed on the circumference of the conduit means a plurality of burners 22, for example, eight burners - but at least one burner on. In a manner not shown each of the burner 22 is connected to the gas supply to the supply line 20.
  • the burners 22 may in this case be oriented such that the gas flowing out of them and initially burning in a flame 24 has a predetermined flow direction component 25 or a flame direction which runs tangentially to the pyrolysis tube 8, so that the pyrolysis tube is heated as evenly as possible.
  • Fig. 2 it is shown that thereby an alignment of the flame 24 of each burner 22 is made possible on the flame 24 of the circumferentially subsequent burner 22. This can be achieved safely and in a structurally simple way that the individual burners 22 of the annular burner ignite each other.
  • the stream of still combusting gases produced by the burners 22 and flue gases already formed by combustion may preferably also have a flow direction component which runs parallel to the longitudinal extent 8c of the pyrolysis tube 8 and opposite to the passage direction of the fuels 2 in the pyrolysis tube.
  • a firing device 21 is shown in which the flame direction 25 of the individual burners 22 are inclined and directed onto the longitudinal axis 8c of the pyrolysis tube.
  • a conduit means 26 described in more detail below is closed at its end 26a in the region of the firing device 21.
  • FIGS. 2 and 3 show extreme positions of the individual burners 22.
  • the burners 22 in FIG. 2 are aligned completely tangentially to the pyrolysis tube 8, the orientation of the flames 24 having no component parallel to the longitudinal axis 8c of the pyrolysis tube.
  • the direction of the flames 24 has no tangential component.
  • the flame direction 25 lies in each case in a sectional plane through the longitudinal axis 8c of the pyrolysis tube.
  • the individual burners of the burner can also occupy any position between the extreme positions shown in the two figures, which can be achieved for example by pivoting the burner shown in Fig. 2 by an angle less than 90 °.
  • a start / support burner 27 is provided in the peripheral region of the annular burner, with which the annular burner can be ignited on the one hand.
  • the flame (not shown) generated by the start / support burner 27 may be directed to at least one of the burners 22 of the annular burner.
  • the start / support burner 27 can also be used if too small amounts of energy are supplied by the ring burner.
  • the start / support burner 27 may be powered by an external fuel supply.
  • the annular burner 26 may be integrated at one end of the conduit means 26 in this.
  • the conduit means 26 may initially be formed as a cross-sectionally annular, substantially rectilinear pipe 28.
  • the annular tube 28 is in this case arranged concentrically around the pyrolysis tube 8.
  • the concentric tube 28 surrounds the pyrolysis tube 8 over its entire length, the longitudinal axes of the two tubes being identical.
  • they In order to allow a good heat transfer from the annular tube to the pyrolysis tube, they have a common tube wall 29 made of a material with good thermal conductivity on. For this purpose, especially metallic materials, such as alloyed steel and cast steel, in question.
  • the annular tube 28 merges at an end opposite the firing device 21 into a first curved region 30 with a deflection angle of 180 °.
  • the one volume of the conduit means fanned into a plurality of individual tubes in a straight line and parallel to each other and to the annular tube 28.
  • this plurality of tubes is shown in FIG. 1 as only a single tube 31. By fanning the total area can be increased at which a heat transfer can take place.
  • a second curvature region 32 is located at an end of the tubes 31 opposite the first curvature region 30.
  • the conduit means is deflected by 180 ° and divided into a further enlarged number of individual tubes 33 (also shown as a single tube) running parallel to one another.
  • a third curvature region 34 then adjoins in the direction of flow, in turn increasing the number of individual tubes. From the third curvature region 34, the conduit means extends to a so-called quenching means 36, which is provided for the shock cooling of the flue gases.
  • the previously described meandering portion (reference numerals 28 to 34) of the conduit means 26 is located approximately from the combustor 21 to the third curvature region 34 in a water-filled closed vessel 37.
  • This section of the conduit means and Boiler 37 thus form a so-called three-pass boiler, which serves for heat recovery.
  • a steam line 38 is connected to these.
  • the resulting due to the heating of the water vapor becomes a Device 39 out, in which the energy content of the water vapor for the production of useful energy, such as electricity, heat or cold, is used.
  • the heat exchanger 28a serves as a heat exchanger 28 a, with which a part of the energy content of the burned gases guided in the tube 28 to the Water of the three-pass boiler is discharged.
  • the heat exchanger 28a absorbs thermal energy from the hot gases on an inner surface 40 of the tube 28 and discharges it to the water on an outer surface 41 of the tube 28.
  • the respective same section of the volumetric flow of the gases simultaneously emits another part of its thermal energy to the pyrolysis tube 8 on an outer surface 42 of the tube wall 29.
  • This part of the thermal energy can be used via an inner surface 43 of the tube wall 29 by radiant heat or by heat transfer to heat the contents of the pyrolysis tube.
  • quenching means the flue gas within a very short time, for example within 0.2 sec. From about 450 ° C to about 200 ° C, cooled.
  • water can be injected into a chamber through which the flue gases are carried out.
  • the quenching process avoids recombinations of the flue gases to dioxins or furans or, at the most, allows them to be harmless enough.
  • the thus cooled flue gases reach a known flue gas cleaning device 45. This has filters with which particles are removed from the flue gas stream. The filtrate, essentially filter dust, is collected in a container 46 for subsequent removal.
  • the thus cleaned flue gas now leaves the flue gas cleaning device 45 and passes over another section 48 of the conduit means to a trained as a suction fan 49 vacuum means.
  • the induced draft fan 49 promotes, on the one hand, the flow of purified flue gas to a chimney 50 provided Rauchgasauslassstelle.
  • the induced draft fan 49 generates at its installation location in the conduit means 26 a negative pressure which can act with respect to a direction opposite to the direction of flow up to the intermediate silo 3.
  • the negative pressure causes a substantially constant volumetric flow of the flue gases through the line 26 closed against the entry of air.
  • the oxygen required for the combustion in the region of the combustor 21 alone due to the negative pressure acting in the combustion device or at least with its support is sucked.
  • the negative pressure for conveying the gas from the gas mixing chamber 12 to the combustor 21 can be used.
  • the system may also be provided with a control device, not shown in the drawing, with the parameters of the emerging from the boiler 37 water vapor can be set as substantially constant.
  • parameters of the steam such as pressure, quantity and temperature, can be measured in the region of the steam outlet, for which reason temperature, quantity and pressure sensors can be present at one or more locations in the steam line.
  • the entry of residues can be increased in a predetermined manner. It can also be provided that in addition the start / support burner is turned on.
  • the combustion temperature of the gases is approximately from 1050.degree. C. to 1150.degree.
  • the temperature is kept as constant as possible within this range, for example at about 1100 ° C. This makes it possible to provide in the pyrolysis tube in a range of 850 ° C to 950 ° C as constant temperature conditions as possible to adjust the available per unit time at the Dampfauslassstelle usable amount of energy as constant as possible.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Processing Of Solid Wastes (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Claims (18)

  1. Installation de production d'énergie, dans laquelle a lieu une valorisation pyrolytique de combustibles contenant du carbone, comprenant
    une partie réactionnelle (8) prévue pour la valorisation du combustible et pourvue d'au moins une zone de pyrolyse, dans laquelle par pyrolyse un gaz est susceptible d'être produit,
    au moins un équipement de combustion (21) avec lequel le gaz produit dans la pyrolyse est susceptible d'être brûlé par alimentation d'oxygène, avec comme résultat la formation de gaz de fumée,
    des moyens d'alimentation (20) destinés à alimenter le gaz provenant de la zone de pyrolyse dans l'un au moins des équipements de combustion (21),
    des moyens formant conduite (26), dans lesquels le gaz en cours de combustion et le gaz de fumée qui en résulte sont susceptibles d'être dirigés depuis l'équipement de combustion (21) vers un poste d'évacuation de gaz, en étant susceptibles d'être guidés dans la zone de pyrolyse, afin d'utiliser l'énergie thermique engendrée avec la combustion, en vue de réchauffer la zone de pyrolyse,
    un équipement d'utilisation de chaleur (39) avec lequel au moins une partie de l'énergie thermique libérée par la combustion est susceptible d'être convertie, par utilisation d'un échangeur de chaleur (28a), en une forme d'énergie utile dégagée par l'installation,
    caractérisée en ce que
    l'équipement d'utilisation de chaleur (39) est disposé de telle façon que le gaz en cours de combustion et/ou le gaz de fumée qui en résulte soit guidé, au moyen d'une section du moyen formant conduite (26) et par rapport au sens d'écoulement, simultanément avec son passage dans la zone de pyrolyse (8) essentiellement aussi au moins le long d'une section d'un échangeur de chaleur (28a), qui absorbe dans une première zone (40) de l'énergie thermique des gaz et restitue celle-ci dans une seconde zone (41) à un fluide de l'équipement d'utilisation de chaleur (39).
  2. Installation selon la revendication 1, caractérisée en ce qu'entre une première surface de délimitation d'une section du moyen formant conduite (26) et une seconde surface de délimitation opposée à ladite première surface de délimitation est ménagé un espace d'écoulement pour les gaz, la zone de pyrolyse (8) venant en limite de la première surface de délimitation et la seconde surface de délimitation étant partie constitutive de l'échangeur de chaleur (28a) .
  3. Installation selon une ou les deux revendications précédentes, caractérisée en ce qu'au moins la section du moyen formant conduite (26) est un tube annulaire (28), qui entoure la zone de pyrolyse (8) et en ce qu'une paroi externe (29) du tube annulaire (28) est une partie constitutive de l'échangeur de chaleur (28a).
  4. Installation selon une ou plusieurs des revendications précédentes 1 à 3, caractérisée en ce que la section du moyen formant conduite (26) est disposée de telle façon qu'au moins une composante du sens d'écoulement du gaz ait un parcours parallèle au développement longitudinal de la zone de pyrolyse (8).
  5. Installation selon la revendication 4, caractérisée en ce qu'au moins la composante du sens d'écoulement est dirigée essentiellement à contre-courant du sens de circulation du combustible dans la zone de pyrolyse.
  6. Installation selon une ou plusieurs des revendications précédentes, caractérisée en ce que par une zone de gazéification située dans la région d'une extrémité de la zone de pyrolyse et dans laquelle par amenée d'oxygène et/ou de matières contenant de l'oxygène a lieu une gazéification de combustibles déjà pyrolysés.
  7. Installation selon la revendication 6, caractérisée en ce que par le moyen d'alimentation de l'équipement de combustion est alimenté le gaz provenant de la zone de pyrolyse, conjointement avec le gaz produit dans la zone de gazéification.
  8. Installation selon la revendication 7, caractérisée en ce qu'en relation avec le sens d'écoulement du gaz de fumée entre l'échangeur de chaleur et la station d'évacuation de gaz est disposé un organe déprimogène, destiné à créer une dépression dans le moyen formant conduite.
  9. Installation selon la revendication 8, caractérisée en ce que l'organe déprimogène est un ventilateur à effet d'aspiration.
  10. Installation selon une ou plusieurs des revendications précédentes, caractérisée en ce que l'échangeur de chaleur est une chaudière multi-voies, en particulier une chaudière à deux ou trois voies.
  11. Installation selon une ou plusieurs des revendications précédentes, caractérisée en ce que par une construction modulaire, selon laquelle des modules fonctionnels de l'installation sont susceptibles d'être fixés à l'installation par des liaisons amovibles et susceptibles d'être retirés de l'installation par escamotage des liaisons.
  12. Procédé pour la production d'énergie, selon lequel a lieu une valorisation pyrolytique de combustibles contenant du carbone, comportant les étapes consistant en :
    un apport de combustibles dans au moins une zone de pyrolyse (8), dans laquelle une pyrolyse est susceptible d'être effectuée,
    une combustion, grâce à une alimentation en oxygène, du gaz généré par la pyrolyse, avec comme résultat la formation de gaz de fumée,
    un transfert du gaz de fumée résultant et provenant de l'équipement de combustion (21), en direction d'un poste d'évacuation de gaz, le gaz en cours de combustion et/ou le gaz de fumée résultant étant susceptible d'être guidé au moyen d'un moyen formant conduite (26) vers la zone de pyrolyse (8), afin d'utiliser l'énergie thermique engendrée avec l'équipement de combustion (21) en vue de réchauffer la zone de pyrolyse (8), et les gaz étant susceptibles d'être guidés vers un équipement d'utilisation de chaleur (28), avec lequel au moins une partie de l'énergie thermique libérée par la combustion est susceptible d'être transformée, par utilisation d'un processus d'échange de chaleur, en une forme d'énergie utile dégagée,
    caractérisé en ce que
    un courant du gaz en cours de combustion et/ou du gaz de fumée résultant est, dans le sens de l'écoulement dans une section du moyen formant conduite, guidé essentiellement de manière simultanée vers la zone de pyrolyse (8) et vers au moins une section d'un échangeur de chaleur (28a), qui absorbe dans une première zone d'échange l'énergie thermique des gaz et qui restitue celle-ci dans une seconde zone d'échange à un fluide de l'équipement d'utilisation de chaleur (28).
  13. Procédé selon la revendication 12, caractérisé en ce que les gaz de fumée dans la première section du moyen formant conduite sont guidés en écoulement aussi bien vers la zone de pyrolyse qu'également vers l'échangeur de chaleur et en ce que dans une seconde section, ils circulent exclusivement dans l'échangeur de chaleur.
  14. Procédé selon une ou les deux revendications précédentes 12 et 13, caractérisé en ce que le fluide est de l'eau et en ce que par le processus d'échange de chaleur de la vapeur d'eau est générée.
  15. Procédé selon une ou plusieurs des revendications précédentes 12 à 14, caractérisé en ce que dans le moyen formant conduite est engendrée une dépression qui est utilisée en vue de la création d'un écoulement des gaz de fumée.
  16. Procédé selon la revendication 15, caractérisé en ce que la dépression destinée au pompage des gaz prévus pour la combustion est utilisée en un emplacement de l'installation, dans laquelle la combustion est effectuée.
  17. Procédé selon une ou plusieurs des revendications précédentes 12 à 16, caractérisé en ce que les combustibles sont, après traversée de la zone de pyrolyse, apportés dans une chambre de gazéification et en ce que dans ladite chambre et par amenée d'oxygène ou de matières contenant de l'oxygène est réalisée par gazéification une production de gaz.
  18. Procédé selon la revendication 12, caractérisé par une étape de régulation, selon laquelle est mesuré un paramètre dépendant du processus d'échange de chaleur et selon laquelle sur la base de cette mesure on fait varier l'apport de combustibles dans l'installation.
EP02708128A 2001-04-12 2002-04-11 Installation et procede pour produire de l'energie par pyrolyse Expired - Lifetime EP1377649B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
CH683012001 2001-04-12
CH6832001 2001-04-12
PCT/CH2002/000202 WO2002083815A1 (fr) 2001-04-12 2002-04-11 Installation et procede pour produire de l'energie par pyrolyse

Publications (2)

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EP1377649A1 EP1377649A1 (fr) 2004-01-07
EP1377649B1 true EP1377649B1 (fr) 2006-06-21

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AT (1) ATE331011T1 (fr)
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WO (1) WO2002083815A1 (fr)

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2666431C (fr) 2006-10-13 2015-09-15 Proterrgo Inc. Procede et appareil pour la gazeification de dechets organiques en lots
WO2010118513A1 (fr) * 2009-04-17 2010-10-21 Proterrgo Inc. Procédé et appareil pour la gazéification de déchets organiques
CN102786951B (zh) * 2012-08-06 2014-03-12 山西鑫立能源科技有限公司 一种煤热解炉的荒煤气导出装置
CN103087783B (zh) * 2012-08-06 2014-02-26 山西鑫立能源科技有限公司 一种煤热解炉的荒煤气导出冷凝及回收净化装置
ITRO20130005A1 (it) * 2013-04-04 2014-10-05 Luca Lazzarin Gassificatore pirolitico per biomassa sigma
CN103232864B (zh) * 2013-04-10 2014-10-08 山西鑫立能源科技有限公司 煤矸石热解气化的荒煤气导出装置
CN103662514B (zh) * 2013-11-07 2015-10-28 潘老省 一种双池垃圾储存库及垃圾处理的方法
CN104819471A (zh) * 2015-05-27 2015-08-05 苏州科锐恒机械科技有限公司 一种垃圾快速焚烧炉
EP3969545A1 (fr) * 2019-03-06 2022-03-23 Next Generation Elements GmbH Procédé pour le recyclage d'au moins une matière de valeur contenue dans une biomasse
AT522257A1 (de) * 2019-03-06 2020-09-15 Next Generation Elements Gmbh Verfahren zur Rückgewinnung zumindest eines in einer Biomasse enthaltenen Wertstoffes

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Publication number Priority date Publication date Assignee Title
DE2651302C3 (de) * 1976-05-12 1981-07-09 PLS Gesellschaft für Pyrolyse-Müllverwertungsverfahren mbH, 8000 München Vorrichtung zur Destillationsgaserzeugung aus Abfall
GB1597517A (en) * 1977-01-07 1981-09-09 Arcalon Gen Petroleum Process and apparatus for the pyrolysis of refuse
DK0874881T3 (da) * 1995-10-26 2000-09-25 Compact Power Ltd Fremstilling af varmeenergi af fast kulholdigt brændsel

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EP1377649A1 (fr) 2004-01-07
WO2002083815A1 (fr) 2002-10-24
ATE331011T1 (de) 2006-07-15
DE50207297D1 (de) 2006-08-03

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