WO2002083815A1 - 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
WO2002083815A1
WO2002083815A1 PCT/CH2002/000202 CH0200202W WO02083815A1 WO 2002083815 A1 WO2002083815 A1 WO 2002083815A1 CH 0200202 W CH0200202 W CH 0200202W WO 02083815 A1 WO02083815 A1 WO 02083815A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
pyrolysis
pyrolysis zone
heat exchanger
combustion
Prior art date
Application number
PCT/CH2002/000202
Other languages
German (de)
English (en)
Inventor
John E. E. Sharpe
Jack R. Metz
Reinhard W. Serchinger
Original Assignee
Fenner, Hans, Rudolf
Gautschi, Ulrich
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Fenner, Hans, Rudolf, Gautschi, Ulrich filed Critical Fenner, Hans, Rudolf
Priority to DE50207297T priority Critical patent/DE50207297D1/de
Priority to EP02708128A priority patent/EP1377649B1/fr
Publication of WO2002083815A1 publication Critical patent/WO2002083815A1/fr

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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 system and a method for generating energy, as described in the preambles of claims 1 and 12.
  • Residual materials include, for example, municipal and industrial waste, recycling sorting waste, waste and residual wood, sewage sludge, animal meal, etc.
  • the pyrolytic processes are based on a degassing of the carbon-containing residues intended as fuels which is carried out at high temperatures and essentially with the exclusion of oxygen.
  • the energy contained in the resulting gases can be burned, e.g. Oxidation that convert gases into thermal energy.
  • Thermal energy is comparatively easy to use, for example to generate heat, cold or electricity.
  • Thermoselect provides for degassing the residues in a temperature range from 450 ° C to 550 ° C.
  • the remaining or partially charred residues from this process then enter a carburetor part of the plant, in which they are gasified with the supply of natural gas and oxygen at 1200 ° C to 2000 ° C.
  • the synthesis gases are then cooled in a wet process and after various cleaning stages for energy generation and with a partial flow for heating the pyrolysis zone
  • the disadvantage of the system is its high level of complexity. Due to the high technical effort required for the process that can be carried out with this plant, only large plants with approx. 100,000 tons of residues per year seem to be profitable.
  • Carbo-V process provides for primarily wood-containing residues to be broken down into their volatile and solid components in a first reactor by partial oxidation.
  • the solid components mainly coal containing coke, are ground.
  • the resulting very tar-containing gas is re-oxidized in the upper part of a combustion chamber, while in the lower part of the combustion chamber the coke dust is converted into raw gasification gas.
  • This gas is cooled and cleaned several times together with the first stage synthesis gas. The cleaned gas is then used to generate 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.
  • this process is essentially only intended for the energy recovery of wood.
  • the invention is therefore based on the object of providing a generic system and a method which enable a good energy balance even with a small system size.
  • This object is achieved according to the invention in a system of the type mentioned at the outset in that the combusting gas and / or the resulting flue gas by means of a section of the line means, and in relation to their direction of flow, at the same time that they pass the pyrolysis zone essentially also at least one Section of a heat exchanger are passed, the heat exchanger absorbing thermal energy of the gases in a first region and delivering it to a medium of the heat utilization device in a second region.
  • the object is also achieved by a method as described in claim 12.
  • a section of a stream of hot combustion or flue gases generated during the combustion is not - as in the prior art - exclusively supplied in succession to different recycling purposes, but preferably already during the combustion and immediately thereafter essentially simultaneously is used both for heating the pyrolysis zone and for delivering thermal energy to a heat exchanger.
  • a further heat transfer should take place, namely a heat transfer at the heat exchanger.
  • this part of the conduction means should advantageously have a particularly good thermal conductivity.
  • predefined physical conditions are created by coordinating the heat transfer at the heat exchanger with the heat transfer to the pyrolysis zone. This is said to be able to reliably maintain the temperature prevailing in the pyrolysis zone at a value which is favorable for pyrolysis within a certain temperature range. This temperature range can be, for example, from 850 ° C to 950 ° C.
  • This temperature range can be, for example, from 850 ° C to 950 ° C.
  • the temperature of the combustion gases during combustion or immediately thereafter in a range from approximately 1000 ° C. to 1200 ° C., preferably from 1050 ° C. to 1150 ° C. and particularly preferably approximately 1100 ° C. , is on the one hand to have good results in the pyrolysis process and on the other hand to have a sufficient amount of energy available for the production of useful energy.
  • This temperature range has also proven to be particularly advantageous since these temperatures, on the one hand, there is certainly no recombination of the combustion or flue gases to form dioxins and furans.
  • the temperatures are high enough to carry the flue gases over a longer distance in the pipe means before they cool down to temperatures at which such recombinations could be feared in significant quantities.
  • a flow space for the can be between a first boundary surface and a second boundary surface of a section of the conduit opposite the first boundary surface Gases are formed.
  • 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 essentially elongated tube which is surrounded by an annular conduit means, the longitudinal extension of which can run essentially parallel to the longitudinal extension of the pyrolysis tube.
  • an (outer) wall of the pyrolysis tube can also function as the inner wall of the conduit, which enables particularly good heat transfer to the pyrolysis zone.
  • an outer wall of the conduit can be designed as a heat exchanger, which also enables particularly good heat transfer to the heat exchange medium with very little heat loss. This also makes it possible to implement a system according to the invention with a particularly low design effort.
  • the pyrolysis tube and the conduit are each circular with respect to their cross-section, the conduit being able to surround the pyrolysis tube concentrically.
  • a plurality of pyrolysis tubes can also be arranged in a conduit which is annular in cross section, the cross-sectional shapes of the conduit and the pyrolysis tubes being able to be optimized with regard to good heat transfer.
  • the cross-sectional shapes of the tubes can be chosen almost arbitrarily.
  • the heat exchanger delivers the energy to a water boiler or boiler, in which water vapor is generated, which in turn can be used to generate a usable form of energy, such as heat, cold or electricity.
  • a water boiler or boiler in which water vapor is generated
  • the line means and thus also the heat exchanger are arranged completely within the water boiler over at least a portion of the line means. This can have the consequence that the pyrolysis zone, at least over a section along a conveying path of the fuel through the pyrolysis zone, is 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 regulate the quantity of residues or fuel fed into the pyrolysis tube so that the values of the steam parameters can be set as essentially constant.
  • FIG. 1 shows a basic structure of a possible system according to the invention
  • FIG. 2 shows a cross-sectional illustration of a ring burner of the system according to the invention
  • Fig. 3 is a longitudinal sectional view of another possible embodiment of a ring burner.
  • Fig. 4 shows a cross section along the line X of Fig. 1 through a pyrolysis tube and part of a heat exchanger.
  • the plant has an input point 1, in which residues 2 can be placed in an intermediate silo 3 of the plant.
  • the intermediate silo 3 is used for the intermediate storage of residues 2 before they are fed to the recycling described in more detail below.
  • a conveyor wheel 4 arranged in a downpipe connects to a lower funnel-shaped end of the intermediate silo.
  • the conveying wheel 4 and / or the residues 2 stored in the silo 3 are essentially airtight on this side of the system.
  • the downpipe opens into the latter in the area of one end of a horizontally oriented pipe 5.
  • a rotary screw conveyor 6 is arranged in the tube 5 and conveys the residual materials 2 into the area of the other end of the tube 5.
  • Also arranged in the pyrolysis tube 8 is a rotatably drivable screw conveyor 9 with which the
  • Residual substances 2 are conveyed from an inlet opening 8a to a lower outlet opening 8b provided at the other end of the pyrolysis tube.
  • the pyrolysis tube 8 is sealed against air entry.
  • the preferably essentially anaerobic pyrolysis process results in temperatures of approximately 850 ° to approximately 950 ° C., preferably approximately 900 ° C., in the interior of the pyrolysis tube.
  • the last-mentioned end of the pyrolysis tube opens into a silo-like container 10 in which a gasification chamber 11 is located below the pyrolysis tube 8 and a gas chamber above it. Mixing chamber 12 is formed.
  • the gasification chamber 11 also belongs to a reaction part of the system. The residues 2, which have passed through the pyrolysis tube 8 and an essentially anaerobic pyrolysis, thus fall due to the force of gravity through the outlet opening 8b of the pyrolysis tube 8 down into the gasification chamber 11 provided with a lower funnel-shaped end.
  • the funnel-shaped end finally opens into another pipe 14 with screw conveyor 15, through which the end products of the gasification process, essentially ash or slag, can be removed from the system in a predetermined amount and time.
  • An arrow 16, 17, 18 indicates three possible introductions with which, alternatively or cumulatively, water vapor (with a temperature of approx. 300 ° C.), recirculated exhaust gas (with a temperature of approx. 200 ° C.) and / or one Oxygen / nitrogen mixture preheated to approx. 200 ° C can be introduced into the gasification chambers. This enables gasification of the already pyrolysed residues or fuels at temperatures of approx. 750 ° C to 850 ° C, whereby the gases hydrogen (H 2 ) and carbon monoxide (CO) can be released, for example.
  • H 2 hydrogen
  • CO carbon monoxide
  • 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 gases formed in the pyrolysis tube for example methane and carbon monoxide, can thus also escape upward through the outlet opening 8b into the gas mixing chamber 12.
  • a feed line 20 connected to the gas mixing chamber 12 the gas mixing chamber is connected to a burner 21 having a ring burner.
  • the combustion device 21 is arranged over the entire circumference of the pyrolysis tube 8 around the latter.
  • the in Fig. 2 in a first exemplary embodiment, a ring burner, shown in more detail in a cross-sectional illustration and arranged laterally directly next to the gas mixing chamber, has a plurality of burners 22, for example eight burners, at least one burner, evenly distributed over the circumference of the line means. In a manner not shown, each of the burners 22 is connected to the supply line 20 for gas supply.
  • the burners 22 can 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 that is tangent to the pyrolysis tube 8, so that the pyrolysis tube is heated as evenly as possible , FIG. 2 shows that this enables the flame 24 of each burner 22 to be aligned with the flame 24 of the burner 22 that follows on the circumference. This can be achieved safely and in a structurally simple manner that the individual burners 22 of the ring burner ignite each other.
  • the stream of gases still burning and the flue gases already generated by the combustion can preferably also have a flow direction component which runs parallel to the longitudinal extension 8c of the pyrolysis tube 8 - and in fact opposite to the flow direction of the fuels 2 in the pyrolysis tube.
  • 3 shows such an embodiment of a combustion device 21, in which the flame direction 25 of the individual burners 22 is inclined and directed towards the longitudinal axis 8c of the pyrolysis tube.
  • a line means 26, which is described in more detail below, is closed at its end 26a in the region of the combustion device 21. Extreme positions of the individual burners 22 are shown in FIGS. 2 and 3. The burners 22 in FIG.
  • the individual burners of the combustion device can also assume any position between the extreme positions shown in the two figures, which can be achieved, for example, by pivoting the burners shown in FIG. 2 through an angle of less than 90 °.
  • a start / support burner 27 is provided in the peripheral region of the ring burner, with which the ring burner can be ignited on the one hand.
  • the flame (not shown) generated by the start / support burner 27 can be directed at at least one of the burners 22 of the ring burner.
  • the start / support burner 27 can also be used if the ring burner supplies too little energy.
  • the start / backup burner 27 can be supplied by an external fuel supply.
  • the ring burner can be integrated into the line means 26 at one end thereof.
  • the conduit 26 can initially be designed as a tube 28 that is ring-shaped in cross section and runs essentially in a straight line.
  • the annular tube 28 is 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.
  • these have a common tube wall 29 made of a material with good thermal conductivity. ability on.
  • Metallic materials such as alloy steel and cast steel, are particularly suitable for this.
  • the annular tube 28 merges at an end opposite the combustion device 21 into a first curvature region 30 with a deflection angle of 180 °.
  • the one volume of the conduit element is fanned out into a plurality of individual straight and parallel tubes that run both to one another and to the annular tube 28.
  • this plurality of tubes is shown as only a single tube 31 in FIG. 1.
  • the fanning out can increase the total area where heat transfer can take place.
  • the conduit is deflected by 180 ° and into a further enlarged number of individual tubes 33 running parallel to one another (likewise as a single tube). provided) divided.
  • a third curvature region 34 then adjoins this in the direction of flow, by again increasing the number of individual tubes.
  • the conduit means runs from the third curvature region 34 to a so-called quenching means 36, which is provided for the shock cooling of the flue gases.
  • the previously described meandering section (reference numerals 28 to 34) of the conduit means 26 is located approximately from the combustion device 21 to the third curvature region 34 in a closed boiler 37 filled with water.
  • This portion of the conduit means and Boiler 37 thus form a so-called three-pass boiler, which is used for heat recovery.
  • a water vapor line 38 is connected to it. This turns the water vapor generated due to the heating of the water into one Device 39 guided, in which the energy content of the water vapor is used to generate useful energy, for example electricity, heat or cold.
  • the heat exchanger 28a serves as a heat exchanger 28a with which part of the energy content of the burned gases guided in the tube 28 is transferred to the Water of the three-pass boiler is released.
  • the heat exchanger 28a absorbs thermal energy from the hot gases on an inner surface 40 of the tube 28 and releases it to the water on an outer surface 41 of the tube 28.
  • the same section of the volume flow of the gases simultaneously releases 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 to heat the contents of the pyrolysis tube via an inner surface 43 of the tube wall 29 by radiant heat or by heat transfer.
  • the flue gas is released within a very short time, for example within 0.2 seconds. from about 450 ° C to about 200 ° C, cooled.
  • water can be injected into a chamber through which the flue gases are also carried out.
  • the quenching process avoids recombinations of the flue gases to form dioxins or furans, or at most permits them to an acceptable degree.
  • the flue gases cooled in this way arrive at a flue gas cleaning device 45 known per se. 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 flue gas thus cleaned now leaves the flue gas cleaning device 45 and arrives via a further outlet. cut 48 of the line means to a vacuum means designed as a suction fan 49.
  • the induced draft fan 49 on the one hand conveys the flow of the cleaned flue gas to a flue gas outlet point provided as a chimney 50.
  • the suction-draft fan 49 generates a negative pressure at its installation point in the conduit means 26, which can act as far as the intermediate silo 3 in a direction opposite to the direction of flow.
  • the negative pressure causes an essentially constant volume flow of the flue gases through the conduit means 26 which are sealed off against the entry of air.
  • the oxygen required for the combustion in the area of the combustion device 21 solely because of the negative pressure also acting in the combustion device or at least with its support is sucked in.
  • the negative pressure can also be used to convey the gas from the gas mixing chamber 12 to the combustion device 21.
  • the system can also be provided with a control device, not shown in the drawing, with which the parameters of the water vapor emerging from the boiler 37 are set as essentially constant.
  • parameters of the steam such as pressure, quantity and temperature
  • 38 temperature, quantity and pressure sensors can be present at one or more points in the steam line.
  • the measured values can then be used to influence the amount of substances entered into the pyrolysis tube 8. For example, if the steam parameters fall or are already too low, the entry of residues can be increased in a predetermined manner. It can also be provided that the start / backup burner is also switched on.
  • the combustion temperature of the gases is approximately from 1050 ° C. to 1150 ° C.
  • the temperature is preferably kept as constant as possible within this range, for example at approximately 1100 ° C. This makes it possible to create temperature conditions that are as constant as possible even in the pyrolysis tube in a range from 850 ° C. to 950 ° C. in order to set the usable amount of energy available per time unit at the steam outlet point as constant as possible.

Abstract

L'invention vise à obtenir un bilan énergétique favorable, même dans des petites installations de production d'énergie dans lesquelles les combustibles carbonés sont mis en valeur par pyrolyse. A cet effet, l'installation comporte les éléments suivants : a) une partie où s'effectue la réaction prévue pour la mise en valeur du combustible, cette partie comprenant au moins une zone de pyrolyse, b) au moins un dispositif de brûlage, qui permet de brûler le gaz de la pyrolyse en gaz de fumée, c) des moyens d'alimentation pour amener le gaz de la zone de pyrolyse dans le dispositif de brûlage, d) des conduites pour transporter le gaz de brûlage et le gaz de fumée obtenu du dispositif de brûlage vers un lieu de décharge des gaz, e) un dispositif d'exploitation thermique qui convertit, au moyen d'un échangeur thermique, au moins une partie de l'énergie thermique dégagée lors du brûlage en énergie utile, que dégage l'installation, étant donné que f) le gaz de brûlage et/ou le gaz de fumée obtenu, au moyen d'une section des conduites (26) et relativement au sens du flux, en passant par la zone de pyrolyse (8), passe simultanément au moins également par une section de l'échangeur thermique (28a), lequel (28a), dans une première partie (40), absorbe l'énergie thermique des gaz qu'il délivre, dans une deuxième partie (41), à un support du dispositif d'exploitation thermique.
PCT/CH2002/000202 2001-04-12 2002-04-11 Installation et procede pour produire de l'energie par pyrolyse WO2002083815A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
DE50207297T DE50207297D1 (de) 2001-04-12 2002-04-11 Anlage und verfahren zur energiegewinnung durch pyrolyse
EP02708128A EP1377649B1 (fr) 2001-04-12 2002-04-11 Installation et procede pour produire de l'energie par pyrolyse

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CH6832001 2001-04-12
CH683/01 2001-04-12

Publications (1)

Publication Number Publication Date
WO2002083815A1 true WO2002083815A1 (fr) 2002-10-24

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Country Link
EP (1) EP1377649B1 (fr)
AT (1) ATE331011T1 (fr)
DE (1) DE50207297D1 (fr)
WO (1) WO2002083815A1 (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2419495A1 (fr) * 2009-04-17 2012-02-22 Proterrgo, Inc. Procédé et appareil pour la gazéification de déchets organiques
CN103232864A (zh) * 2013-04-10 2013-08-07 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
CN103662514A (zh) * 2013-11-07 2014-03-26 潘老省 一种双池垃圾储存库及垃圾处理的方法
ITRO20130005A1 (it) * 2013-04-04 2014-10-05 Luca Lazzarin Gassificatore pirolitico per biomassa sigma
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
US9139785B2 (en) 2006-10-13 2015-09-22 Proterrgo, Inc. Method and apparatus for gasification of organic waste in batches
WO2020176917A1 (fr) * 2019-03-06 2020-09-10 Next Generation Elements Gmbh Procédé pour le recyclage d'au moins une matière de valeur contenue dans une biomasse
AT522258A1 (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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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

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Cited By (12)

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Publication number Priority date Publication date Assignee Title
US9139785B2 (en) 2006-10-13 2015-09-22 Proterrgo, Inc. Method and apparatus for gasification of organic waste in batches
EP2419495A1 (fr) * 2009-04-17 2012-02-22 Proterrgo, Inc. Procédé et appareil pour la gazéification de déchets organiques
JP2012523948A (ja) * 2009-04-17 2012-10-11 プロターゴ インコーポレーテッド 有機廃棄物のガス化方法およびその装置
EP2419495A4 (fr) * 2009-04-17 2013-11-13 Proterrgo Inc Procédé et appareil pour la gazéification de déchets organiques
AU2010237560B2 (en) * 2009-04-17 2015-09-10 Proterrgo Inc. Method and apparatus for gasification of organic waste
US9657941B2 (en) 2009-04-17 2017-05-23 Proterrgo Inc. Method and apparatus for gasification of organic waste
ITRO20130005A1 (it) * 2013-04-04 2014-10-05 Luca Lazzarin Gassificatore pirolitico per biomassa sigma
CN103232864A (zh) * 2013-04-10 2013-08-07 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
CN103662514A (zh) * 2013-11-07 2014-03-26 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
WO2020176917A1 (fr) * 2019-03-06 2020-09-10 Next Generation Elements Gmbh Procédé pour le recyclage d'au moins une matière de valeur contenue dans une biomasse
AT522258A1 (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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EP1377649B1 (fr) 2006-06-21

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