EP0749551A1 - Process for the heat treatment of waste material - Google Patents

Process for the heat treatment of waste material

Info

Publication number
EP0749551A1
EP0749551A1 EP96900074A EP96900074A EP0749551A1 EP 0749551 A1 EP0749551 A1 EP 0749551A1 EP 96900074 A EP96900074 A EP 96900074A EP 96900074 A EP96900074 A EP 96900074A EP 0749551 A1 EP0749551 A1 EP 0749551A1
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
afterburning
solid
chamber
separated
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.)
Granted
Application number
EP96900074A
Other languages
German (de)
French (fr)
Other versions
EP0749551B1 (en
Inventor
Patrick Müller
Hans Rüegg
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hitachi Zosen Innova AG
Original Assignee
Von Roll Umwelttechnik AG
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 Von Roll Umwelttechnik AG filed Critical Von Roll Umwelttechnik AG
Publication of EP0749551A1 publication Critical patent/EP0749551A1/en
Application granted granted Critical
Publication of EP0749551B1 publication Critical patent/EP0749551B1/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

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
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • 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

Definitions

  • the invention relates to a method for the thermal treatment of waste material with the production of thermal energy according to the preamble of claim 1.
  • Degassing as a thermal process for generating energy from waste also known as pyrolysis, smoldering or coking
  • pyrolysis also known as pyrolysis
  • smoldering or coking
  • the waste is heated in the absence of oxygen by direct or indirect heat supply.
  • the organic compounds in the waste become unstable; the volatiles escape and the non-volatiles are converted to coke.
  • the smoldering gases generated during degassing have a high calorific value.
  • these smoldering gases are burned directly in the conventional post-combustion chambers with oxygen or oxygen-enriched air, very high, difficult to control temperatures of over 2000 ° C arise.
  • the present invention has for its object to provide a method of the type mentioned, which allows control of the temperature profile in the afterburning.
  • the process according to the invention is pyrolysis of waste, in particular waste, in which w already mentioned very high temperatures arise in the afterburning with oxygen;
  • the afterburning according to the invention in a circulating fluidized bed creates optimal and uniform reaction conditions for the afterburning, and a very homogeneous temperature distribution is achieved.
  • very efficient cooling of the hot carbonization gases is achieved.
  • the gas-solid flow in the fluidized bed results in very good heat transfer, which leads to a reduction in the heat transfer area and thus also in the boiler volume.
  • the reduction in the amount of flue gas achieved by the afterburning with oxygen also causes a reduction in the construction volume of the fluidized bed reactor and the downstream units, an increase in size Boiler efficiency, an on-reduction for gas cleaning and a reduction in the risk of corrosion of the heat transfer surfaces.
  • the unreacted ammonia in the flue gas is called slip and represents an environmental impact. If the temperature is too high, some of the ammonia burns. In both cases, the amount of ammonia required is unnecessarily high.
  • the temperature of the flue gases decreases continuously along the flue gas path through the afterburning chamber and boiler. The ammonia is introduced at the optimal flue gas temperature.
  • the flue gas temperature profile depends on the operating state of the system and on the waste material burned. This means that the location of the optimal discharge point also depends on the operating state of the furnace.
  • the design of the afterburner chamber as a circulating fluidized bed enables a solution to the problem of choosing the ammonia inlet point for the smoke Winding.
  • the circulating fluidized bed is characterized not only by constant temperature but also by good temperature control behavior. For example, the flow of solid matter diverted into the fluid bed cooler can be regulated. This allows regulation of the heat flow also removed from the afterburning chamber and thus precise regulation of the temperature in the afterburning comb, regardless of the operating state of the furnace in the pyrolysis chamber. This means that a fixed ammonia inlet point can be selected, since the flue gas temperature profile in the afterburning chamber and boiler no longer depends on the operating state of the furnace. This also enables a minimization of the ammonia consumption for nitrogen oxide reduction by choosing an optimal temperature i of the afterburning chamber and this independently of the operating state in the pyrolysis chamber.
  • FIG. 1 shows a flow diagram of a first method variant
  • waste materials are subjected to degassing in a pyrolysis chamber 2 in a manner known per se and not shown in detail.
  • the waste supply is indicated by an arrow 1.
  • the waste supply and the degassing can take place, for example, in the manner described in Swiss patent application No. 01 510 / 94-8 (A 10364 CH).
  • Smoldering gases formed during the degassing enter an afterburning chamber 4a (the transition from pyrolysis chamber 2 to afterburning chamber 4a is indicated by an arrow 3), which according to the invention is designed as a fluidized bed reactor.
  • the carbonization gases used as fluidizing gases are re-burned with the addition of oxygen (indicated by arrow 5 in FIG. 1).
  • Lime, sand and other materials can be used as the fluidized bed solid;
  • the refuse coke obtained in the pyrolysis - freed from inert substances and finely ground - can be introduced into the fluidized bed in particle form and also burned there.
  • the walls of the afterburning chamber 4a are designed as cooling or heat transfer surfaces; at most, further heat transfer surfaces can be arranged directly in the fluidized bed. These heat transfer surfaces are symbolically designated 6 in FIG. 1.
  • the fluidized bed reactor is operated at such a high gas velocity that at least some of the solid particles are discharged together with the flue gas stream from the afterburning chamber 4a. Arrived via a line 7 in a dust separator 8, the solid is separated from the flue gas stream.
  • the dust separator 8 can be designed, for example, as a cyclone, a dust filter or as an electrostatic filter.
  • the secluded Solid is returned via line 9 into the afterburning comb 4a, so that a circulating fluidized bed is formed.
  • the freed from the solid and cooled flue gases flow via a line 10 further flue gas cleaning or flue gas cooling devices, not shown, before they reach the atmosphere.
  • the circulating fluidized bed is expanded by an external fluid bed cooler 1.
  • This allows a part of the heat dissipation a of the afterburning chamber 4b to be outsourced.
  • Part of the dust separator 8 separated solid is diverted via line 13 into the fluidized bed cooler 12, where in a stationary fluidized bed (fluidized bed) is cooled by direct or indirect heat transfer (corresponding heat transfer surfaces of the fluidized bed cooler 12 are symbolically designated 15) and then via a line 14 reaches the afterburning chamber again.
  • this solid absorbs the heat from the hot carbonization gases and heats up to the mixing temperature prevailing in the afterburning chamber 4b.
  • there is no need for additional cooling surfaces in the afterburning chamber since the recirculated part of the solid which is cooled in the fluid bed 12 takes over the cooling function.
  • a fluidizing gas required for the operation of the fluidized bed cooler 12 is fed to the fluidized bed cooler 12 via line 16 and withdrawn for further use above the fluidized bed (line 17).
  • the entire solid separated from the flue gas flow in the dust separator 8 is passed through the fluidized bed cooler 12 and recirculated cooled into the fluidized bed of the afterburning chamber 4c.
  • a large amount of cooled solid is introduced into the fluidized bed so that the afterburning of the carbonization gases can be carried out at a low temperature level of approx. 900 ° C .; the average suspension density is at least 20-50 kg / Nm.
  • the suspension density of the gas-solid mixture must be selected to be significantly higher, for example 50-100 kg / Nm 3 , in order to ensure sufficient heat transfer to the walls of the boiler To ensure fluidized bed reactor.
  • the temperature in the afterburning chamber 4b or 4c can be precisely regulated independently of the operating state in the pyrolysis chamber 2 by regulating the entry of the solid cooled in the fluidized bed cooler 12.
  • This enables ammonia as a reducing agent for nitrogen oxide separation into the afterburning chamber 4b or 4c or can be optimally passed into the dust separator 8 or cyclone, and that the temperature is selected so that the nitrogen oxide separation can be carried out with minimal ammonia consumption.
  • the ammonia is preferably introduced into the cyclone inlet.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Processing Of Solid Wastes (AREA)
  • Closures For Containers (AREA)
  • Treatment Of Sludge (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)

Abstract

The waste material is degassed under the action of heat in a pyrolysis chamber (2). Volatile degassing products undergo post-combustion in a post-combustion chamber (4a, 4b or 4c) in the form of a fluidized bed reactor as oxygen is fed in. The solid matter discharged from the post-combustion chamber (4a, 4b or 4c) is separated from the flue gas stream in a dust trap (8) and fed back into the post-combustion chamber (4a, 4b or 4c) preferably after being cooled in an external fluidized bed cooler. The temperatures of more than 2500 °C produced by the post-combustion of low-temperature carbonization gases with high calorific values (at least 8000 kilojoules/Nm3) can be kept under control.

Description

Verfahren zur thermischen Behandlung von AbfallmaterialProcess for the thermal treatment of waste material
Die Erfindung betrifft ein Verfahren zur thermischen Behandlung von Abfallmaterial unter Gewinnung thermischer Energie gemäss dem Oberbegriff des Anspruches 1.The invention relates to a method for the thermal treatment of waste material with the production of thermal energy according to the preamble of claim 1.
Die Entgasung als ein thermisches Verfahren zur Energie¬ gewinnung aus Abfall, auch Pyrolyse, Schwelung oder Ver¬ kokung genannt, ist bekannt (vgl. azu Fachzeitschrift Müll und Abfall 12/1978 oder Schweizerisches Patentgesuch Nr. 01 510/94-8, A 10364 CH) . Bei allen auf Entgasung basierenden Verfahren wird der Abfall unter Sauerstoff- ausschluss durch direkte oder auch indirekte Wärmezufuhr erhitzt. Dabei werden die organischen Verbindungen im Abfall instabil; die flüchtigen Bestandteile entweichen, und die nicht flüchtigen werden in Koks umgewandelt.Degassing as a thermal process for generating energy from waste, also known as pyrolysis, smoldering or coking, is known (cf. a specialist journal Müll und Abfall 12/1978 or Swiss patent application No. 01 510 / 94-8, A 10364 CH). In all processes based on degassing, the waste is heated in the absence of oxygen by direct or indirect heat supply. The organic compounds in the waste become unstable; the volatiles escape and the non-volatiles are converted to coke.
Die bei der Entgasung entstehenden Schwelgase haben einen hohen Heizwert. Bei einer direkten Verbrennung dieser Schwelgase in den herkömmlichen Nachbrennkammern mit Sauerstoff oder sauerstoffangereicherter Luft entstehen sehr hohe, schwer beherrschbare Temperaturen von über 2000°C.The smoldering gases generated during degassing have a high calorific value. When these smoldering gases are burned directly in the conventional post-combustion chambers with oxygen or oxygen-enriched air, very high, difficult to control temperatures of over 2000 ° C arise.
Der vorliegenden Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art zu schaffen, das eine Beherrschung des Temperaturprofils bei der Nachverbrennung ermöglicht.The present invention has for its object to provide a method of the type mentioned, which allows control of the temperature profile in the afterburning.
Diese Aufgabe wird erfindungsgemäss durch die im Kenn¬ zeichen des Anspruches 1 angegebenen Merkmale gelöst. Aus der DE-OS 33 07 848 ist es bekannt, brennba Bestandteile enthaltende Prozessabgase aus der Metalurg in einer zirkulierenden Wirbelschicht nachzuverbrenn und zu reinigen, wobei die Prozessabgase und saue stoffhaltige Gase getrennt in den Wirbelschichtreakt eingeleitet werden, und darin in Gegenwart von Ga reinigunsmittel enthaltendem Feststoff nachverbrannt u gleichzeitig gereinigt werden. Die eingesetzten Prozes abgase haben einen niedrigen Heizwert.According to the invention, this object is achieved by the features specified in the characterizing part of claim 1. From DE-OS 33 07 848 it is known to afterburn and clean combustible constituent process gases from the metallurgy in a circulating fluidized bed, the process exhaust gases and acid-containing gases being introduced separately into the fluidized bed react, and in the presence of Ga containing detergents Solid burned and cleaned at the same time. The process gases used have a low calorific value.
Aus der WO-A-93/18341 ist es bekannt, homogene Bren stoffe wie Kohle, Öl oder Petroleumkoks in zwei getren ten Stufen zu verbrennen. Dabei erfolgt die Verbrennu in beiden Stufen unter Sauerstoffzufuhr. Um die in d ersten Stufe nicht verbrannten Feststoffe, d.h. Kohle stoff und Gase, zu verbrennen, wird in der zweiten Stu ein Sauerstoffüberschuss eingesetzt.From WO-A-93/18341 it is known to burn homogeneous fuels such as coal, oil or petroleum coke in two stages. The combustion takes place in both stages with the addition of oxygen. For the solids not burned in the first stage, i.e. To burn carbon and gases, an excess of oxygen is used in the second stage.
Beim erfindungsgemässen Verfahren handelt es sich Pyrolyse von Abfall, insbesondere Müll, bei welcher w bereits erwähnt bei der Nachverbrennung mit Sauersto sehr hohe Temperaturen entstehen; durch die erfi dungsgemässe Nachverbrennung in einer zirkulierend Wirbelschicht werden optimale und einheitliche Rea tionsbedingungen für die Nachverbrennung geschaffen, eine sehr homogene Temperaturverteilung erreicht wir Gleichzeitig wird eine sehr effiziente Kühlung de heissen Schwelgase erzielt. Die in der Wirbelschich vorhandene Gas-FeststoffStrömung ergibt einen sehr gute Wärmeübergang, was zu einer Verkleinerung der Wärme übertragungsflächen und damit auch des Kessel-Bauvolumen führt. Auch die durch die Nachverbrennung mit Sauerstof erreichte Rauchgasmengenreduktion bewirkt eine Verklei nerung des Bauvolumens des Wirbelschichtreaktors und de nachgeschalteten Aggregate, eine Vergrösserung de Kesselwirkungsgrades, eine Auf andreduktion für Gas¬ reinigung und eine Herabsetzung der Korrosionsgefahr der Wärmeübertragungsflächen.The process according to the invention is pyrolysis of waste, in particular waste, in which w already mentioned very high temperatures arise in the afterburning with oxygen; The afterburning according to the invention in a circulating fluidized bed creates optimal and uniform reaction conditions for the afterburning, and a very homogeneous temperature distribution is achieved. At the same time, very efficient cooling of the hot carbonization gases is achieved. The gas-solid flow in the fluidized bed results in very good heat transfer, which leads to a reduction in the heat transfer area and thus also in the boiler volume. The reduction in the amount of flue gas achieved by the afterburning with oxygen also causes a reduction in the construction volume of the fluidized bed reactor and the downstream units, an increase in size Boiler efficiency, an on-reduction for gas cleaning and a reduction in the risk of corrosion of the heat transfer surfaces.
Ein Problem bei thermischer Behandlung von Abfall ist die Entstehung von Stickoxiden. Diese können aus Gründen des Umweltschutzes nicht frei an die Umgebung abgegeben werden. Es sind bereits mehrere Verfahren bekannt, so z.B. das SNCR-Verfahren (Selective Noncatalytic Reduction Process), siehe US-PS 3,970,739, bei welchem Stickoxide in Rauchgasen durch Einsprühen einer Ammoniaklösung oder anderer geeigneter Reduktionsmittel, in Gegenwart des ohnehin vorhandenen Sauerstoffs, zu Stickstoff reduziert werden. Das Ammoniak wird dazu üblicherweise an geeigneter Stelle in den Rauchgasstrom eingeleitet. Dabei spielt die Rauchgastemperatur an der Einleitstelle eine grosse Rolle. Sie muss zwischen 700° und 1100°C liegen. Bei zu niedriger Rauchgastemperatur wird ein grosser Ammoniakuberschuss benötigt. Das nichtreagierte Ammoniak im Rauchgas wird als Schlupf bezeichnet und stellt eine Umweltbelastung dar. Bei zu hoher Temperatur verbrennt ein Teil des Ammoniaks. In beiden Fällen ist die benötigte Ammoniakmenge unnötig hoch. Entlang des Rauchgasweges durch Nachbrennkammer und Kessel nimmt die Temperatur der Rauchgase kontinuierlich ab. Das Ammoniak wird an der Stelle optimaler Rauchgastemperatur einge¬ leitet. Dabei stellt sich jedoch das Problem, dass das Rauchgastemperaturprofil vom Betriebszustand der Anlage und vom verbrannten Abfallmaterial abhängt. Das bedeutet, dass auch die Lage der optimalen Einleitstelle vom Betriebszustand der Feuerung abhängt.One problem with thermal treatment of waste is the formation of nitrogen oxides. For reasons of environmental protection, these cannot be freely released into the environment. Several methods are already known, e.g. the SNCR process (Selective Noncatalytic Reduction Process), see US Pat. No. 3,970,739, in which nitrogen oxides in flue gases are reduced to nitrogen by spraying in an ammonia solution or other suitable reducing agents, in the presence of the oxygen which is already present. The ammonia is usually introduced into the flue gas stream at a suitable point. The flue gas temperature at the inlet point plays a major role. It must be between 700 ° and 1100 ° C. If the flue gas temperature is too low, a large excess of ammonia is required. The unreacted ammonia in the flue gas is called slip and represents an environmental impact. If the temperature is too high, some of the ammonia burns. In both cases, the amount of ammonia required is unnecessarily high. The temperature of the flue gases decreases continuously along the flue gas path through the afterburning chamber and boiler. The ammonia is introduced at the optimal flue gas temperature. However, the problem arises here that the flue gas temperature profile depends on the operating state of the system and on the waste material burned. This means that the location of the optimal discharge point also depends on the operating state of the furnace.
Die Ausgestaltung der Nachbrennkammer als zirkulierende Wirbelschicht ermöglicht eine Lösung des Problems der Wahl der Ammoniak-Einleitstelle für die Rauchgasent- Wicklung. Die zirkulierende Wirbelschicht zeichnet sic neben der Temperaturkonstanz auch durch ein gute Temperaturregelverhalten aus. So kann z.B. der in de Fliessbettkühler umgeleitete Feststoffmengenstro geregelt werden. Dies erlaubt eine Regelung des auch de Nachbrennkammer abgeführten Wärmestroms und damit ein genaue Regelung der Temperatur in der Nachbrennkamme unabhängig vom Betriebszustand der Feuerung in de Pyrolysekammer. Dadurch kann eine feste Ammoniak Einleitstelle gewählt werden, da das Rauchgastemperatur profil in Nachbrennkammer und Kessel nicht mehr vo Betriebszustand der Feuerung abhängt. Dies ermöglich zudem eine Minimierung des Ammoniakverbrauchs zur Stick oxidminderung durch Wahl einer optimalen Temperatur i der Nachbrennkammer und dies unabhängig vom Betriebs zustand in der Pyrolysekammer.The design of the afterburner chamber as a circulating fluidized bed enables a solution to the problem of choosing the ammonia inlet point for the smoke Winding. The circulating fluidized bed is characterized not only by constant temperature but also by good temperature control behavior. For example, the flow of solid matter diverted into the fluid bed cooler can be regulated. This allows regulation of the heat flow also removed from the afterburning chamber and thus precise regulation of the temperature in the afterburning comb, regardless of the operating state of the furnace in the pyrolysis chamber. This means that a fixed ammonia inlet point can be selected, since the flue gas temperature profile in the afterburning chamber and boiler no longer depends on the operating state of the furnace. This also enables a minimization of the ammonia consumption for nitrogen oxide reduction by choosing an optimal temperature i of the afterburning chamber and this independently of the operating state in the pyrolysis chamber.
Die Erfindung wird nun anhand der Zeichnung näher erläu tert. Drei Varianten des erfindungsgemässen Verfahren sind in der Zeichnung dargestellt und im folgenden nähe beschrieben.The invention will now be explained in more detail with reference to the drawing. Three variants of the method according to the invention are shown in the drawing and are described in the following.
Es zeigen:Show it:
Fig.1 ein Fliessschema einer ersten Verfahrens¬ variante;1 shows a flow diagram of a first method variant;
Fig.2 ein Fliessschema einer zweiten Verfahrens¬ variante;2 shows a flow diagram of a second method variant;
Fig.3 ein Fliessschema einer dritten Verfahrens¬ variante. Gemäss Fig. 1 werden Abfallstoffe in einer an sich bekannten und nicht näher dargestellten Weise in einer Pyrolysekammer 2 einer Entgasung unterzogen. Die Abfall¬ zufuhr ist mit einem Pfeil 1 bezeichnet. Die Abfallzufuhr und die Entgasung kann beispielsweise in der im schweizerischen Patentgesuch Nr.01 510/94-8 (A 10364 CH) beschriebenen Art und Weise erfolgen. Bei der Entgasung entstehende Schwelgase treten in eine Nachbrennkammer 4a ein (der Übergang von Pyrolysekammer 2 zur Nachbrenn¬ kammer 4a ist mit einem Pfeil 3 bezeichnet), die erfindungsgemäss als ein Wirbelschichtreaktor ausgebildet ist. In der Nachbrennkammer 4a werden die als Fluidi- sierungsgase eingesetzten Schwelgase unter Sauer¬ stoffzufuhr (in Fig.1 mit Pfeil 5 angedeutet) nach¬ verbrannt. Als Wirbelschicht-Feststoff kann Kalk, Sand und andere Materialien verwendet werden; in einer bevorzugten Weise kann auch der bei der Pyrolyse anfallende Müllkoks - von Inertstoffen befreit und fein aufgemahlen - in Partikelform in die Wirbelschicht eingetragen und dort mitverbrannt werden.3 shows a flow diagram of a third method variant. 1, waste materials are subjected to degassing in a pyrolysis chamber 2 in a manner known per se and not shown in detail. The waste supply is indicated by an arrow 1. The waste supply and the degassing can take place, for example, in the manner described in Swiss patent application No. 01 510 / 94-8 (A 10364 CH). Smoldering gases formed during the degassing enter an afterburning chamber 4a (the transition from pyrolysis chamber 2 to afterburning chamber 4a is indicated by an arrow 3), which according to the invention is designed as a fluidized bed reactor. In the afterburning chamber 4a, the carbonization gases used as fluidizing gases are re-burned with the addition of oxygen (indicated by arrow 5 in FIG. 1). Lime, sand and other materials can be used as the fluidized bed solid; In a preferred manner, the refuse coke obtained in the pyrolysis - freed from inert substances and finely ground - can be introduced into the fluidized bed in particle form and also burned there.
Die Wände der Nachbrennkammer 4a sind als Kühl- bzw. Wärmeübertragungsflächen ausgestaltet; allenfalls können weitere Wärmeübertragungsflächen direkt in der Wirbel¬ schicht angeordnet werden. Diese Wärmeübertragungsflächen sind in Fig. 1 symbolisch mit 6 bezeichnet.The walls of the afterburning chamber 4a are designed as cooling or heat transfer surfaces; at most, further heat transfer surfaces can be arranged directly in the fluidized bed. These heat transfer surfaces are symbolically designated 6 in FIG. 1.
Der Wirbelschichtreaktor wird mit einer derart grossen Gasgeschwindigkeit betrieben, dass zumindest ein Teil der Feststoffpartikel zusammen mit dem Rauchgasstrom aus der Nachbrennkammer 4a ausgetragen wird. Über eine Leitung 7 in einem Staubabscheider 8 angelangt wird der Feststoff vom Rauchgasstrom getrennt. Der Staubabscheider 8 kann z.B. als ein Zyklon, ein Staubfilter oder als ein Elektrofilter ausgebildet werden. Der abgeschiedene Feststoff wird über eine Leitung 9 in die Nachbrennkamm 4a zurückgeführt, so dass eine zirkulierende Wirbe schicht entsteht. Die vom Feststoff befreiten u gekühlten Rauchgase strömen über eine Leitung 10 weiteren, nicht dargestellten Rauchgasreinigungs- bz Rauchgaskühlungseinrichtungen, bevor sie in d Atmosphäre gelangen.The fluidized bed reactor is operated at such a high gas velocity that at least some of the solid particles are discharged together with the flue gas stream from the afterburning chamber 4a. Arrived via a line 7 in a dust separator 8, the solid is separated from the flue gas stream. The dust separator 8 can be designed, for example, as a cyclone, a dust filter or as an electrostatic filter. The secluded Solid is returned via line 9 into the afterburning comb 4a, so that a circulating fluidized bed is formed. The freed from the solid and cooled flue gases flow via a line 10 further flue gas cleaning or flue gas cooling devices, not shown, before they reach the atmosphere.
Gemäss Fig. 2, in der die aus Fig. 1 bekannten u gleichbleibenden Teile des Fliessschemas mit den gleich Bezugsziffern bezeichnet sind, ist die zirkulieren Wirbelschicht um einen externen Fliessbettkühler 1 erweitert. Dieser erlaubt, einen Teil der Wärmeabfuhr a der Nachbrennkammer 4b auszulagern. Ein Teil des Staubabscheider 8 abgesonderten Feststoffes wird üb Leitung 13 in den Fliessbettkühler 12 umgeleitet, wo in einer stationären Wirbelschicht (Fliessbett) dur direkten oder indirekten Wärmeübergang abgekühlt wi (entsprechende Wärmeübertragungsflächen des Fliessbet kühlers 12 sind mit 15 symbolisch bezeichnet) und dana über eine Leitung 14 erneut in die Nachbrennkammer gelangt. In der Nachbrennkammer 4b nimmt dieser Feststo die Wärme aus den heissen Schwelgasen auf und erwär sich auf die in der Nachbrennkammer 4b herrschen Mischtemperatur. Bei dieser Variante kann auf d zusätzlichen Kühlungsflächen in der Nachbrennkammer verzichtet werden, da der rezirkulierte, im Fliessbet kühler 12 gekühlte Teil des Feststoffes die Kühlung funktion übernimmt.According to FIG. 2, in which the parts of the flow diagram known from FIG. 1 that are the same are designated by the same reference numerals, the circulating fluidized bed is expanded by an external fluid bed cooler 1. This allows a part of the heat dissipation a of the afterburning chamber 4b to be outsourced. Part of the dust separator 8 separated solid is diverted via line 13 into the fluidized bed cooler 12, where in a stationary fluidized bed (fluidized bed) is cooled by direct or indirect heat transfer (corresponding heat transfer surfaces of the fluidized bed cooler 12 are symbolically designated 15) and then via a line 14 reaches the afterburning chamber again. In the afterburning chamber 4b, this solid absorbs the heat from the hot carbonization gases and heats up to the mixing temperature prevailing in the afterburning chamber 4b. In this variant, there is no need for additional cooling surfaces in the afterburning chamber, since the recirculated part of the solid which is cooled in the fluid bed 12 takes over the cooling function.
Ein für den Betrieb des Fliessbettkühlers 12 benötigt Fluidisierungsgas wird dem Fliessbettkühler 12 über ei Leitung 16 zugeführt und oberhalb des Fliessbettes einer weiteren Verwendung wieder abgezogen (Leitung 17). Bei der in Fig. 3 dargestellten Variante wird der gesamte, vom Rauchgasstrom im Staubabscheider 8 abgesonderte Feststoff durch den Fliessbettkühler 12 geleitet und gekühlt in die Wirbelschicht der Nachbrenn¬ kammer 4c rezirkuliert.A fluidizing gas required for the operation of the fluidized bed cooler 12 is fed to the fluidized bed cooler 12 via line 16 and withdrawn for further use above the fluidized bed (line 17). In the variant shown in FIG. 3, the entire solid separated from the flue gas flow in the dust separator 8 is passed through the fluidized bed cooler 12 and recirculated cooled into the fluidized bed of the afterburning chamber 4c.
Durch die Verlagerung der ansonsten am stärksten von Korrosionserscheinungen betroffenen Wärmeübertragungs¬ flächen in den Fliessbettkühler 12 (Fig. 2 und 3) wird eine starke Verminderung der Kesselkorrosion erreicht. Im Fliessbettkühler 12 werden die Wärmeübertragungsflächen 15 weniger der Korrosion ausgesetzt, da hier die stark korrosiv wirkenden Rauchgase gar nicht zum Einsatz kommen.By relocating the heat transfer surfaces, which are otherwise most affected by corrosion, into the fluidized bed cooler 12 (FIGS. 2 and 3), a strong reduction in boiler corrosion is achieved. In the fluidized bed cooler 12, the heat transfer surfaces 15 are less exposed to corrosion, since the highly corrosive smoke gases are not used here.
Bei den in Fig. 2 und 3 dargestellten Verfahrungs- varianten wird eine grosse Menge gekühlten Feststoffes in die Wirbelschicht eingetragen, damit die Nachverbrennung der Schwelgase auf niedrigem Temperaturniveau von ca. 900°C durchgeführt werden kann; die mittlere Suspen¬ sionsdichte liegt mindestens bei 20-50 kg/Nm . Wird auf den Fliessbettkühler 12 verzichtet (Variante nach Fig. 1 ) , so muss die Suspensionsdichte der Gas-Feststoff¬ mischung noch wesentlich höher gewählt werden, z.B. 50- 100 kg/Nm3 , um einen genügenden Wärmeübergang an die als Kessel ausgestalteten Wände des Wirbelschichtreaktors zu gewährleisten.In the process variants shown in FIGS. 2 and 3, a large amount of cooled solid is introduced into the fluidized bed so that the afterburning of the carbonization gases can be carried out at a low temperature level of approx. 900 ° C .; the average suspension density is at least 20-50 kg / Nm. If the fluid bed cooler 12 is dispensed with (variant according to FIG. 1), the suspension density of the gas-solid mixture must be selected to be significantly higher, for example 50-100 kg / Nm 3 , in order to ensure sufficient heat transfer to the walls of the boiler To ensure fluidized bed reactor.
Bei den in Fig. 2 und 3 dargestellten Verfahrensvarianten kann die Temperatur in der Nachbrennkammer 4b bzw. 4c unabhängig vom Betriebszustand in der Pyrolysekammer 2 genau geregelt werden, indem der Eintrag des im Fliess¬ bettkühler 12 gekühlten Feststoffes geregelt wird. Dies ermöglicht, dass Ammoniak als Reduktionsmittel zur Stickoxidabscheidung in die Nachbrennkammer 4b bzw. 4c oder in den Staubabscheider 8 bzw. Zyklon optimal ei geleitet werden kann, und dass die Temperatur so gewäh wird, dass die Stickoxidabscheidung mit minimal Ammoniakverbrauch durchgeführt werden kann. Vorzugswei wird der Ammoniak in den Zykloneinlauf eingeleitet. In the process variants shown in FIGS. 2 and 3, the temperature in the afterburning chamber 4b or 4c can be precisely regulated independently of the operating state in the pyrolysis chamber 2 by regulating the entry of the solid cooled in the fluidized bed cooler 12. This enables ammonia as a reducing agent for nitrogen oxide separation into the afterburning chamber 4b or 4c or can be optimally passed into the dust separator 8 or cyclone, and that the temperature is selected so that the nitrogen oxide separation can be carried out with minimal ammonia consumption. The ammonia is preferably introduced into the cyclone inlet.

Claims

Patentansprüche claims
1. Verfahren zur thermischen Behandlung von Abfall¬ material unter Gewinnung thermischer Energie, wobei das Abfallmaterial unter Wärmeeinwirkung entgast wird und als festes Entgasungsprodukt brennbarer Koks und als flüchtiges Entgasungsprodukt brennbare Gase, die anschliessend zur Wärmegewinnung nachverbrannt werden, erzeugt werden, dadurch gekennzeichnet, dass die brennbaren Gase in einer zirkulierenden Wirbelschicht unter Sauerstoffzufuhr nachverbrannt werden, wobei der aus der Wirbelschicht ausgetragene Feststoff vom Rauchgas abgetrennt (8) erneut in die Nachverbrennung (4a bzw. 4b bzw. 4c) zurückgeführt wird.1. A method for the thermal treatment of waste material with the production of thermal energy, the waste material being degassed under the action of heat and generating combustible coke as a solid degassing product and combustible gases as a volatile degassing product, which are subsequently burned for heat recovery, characterized in that the combustible gases are subsequently burned in a circulating fluidized bed with the addition of oxygen, the solid discharged from the fluidized bed being separated from the flue gas (8) and recycled again to the afterburning (4a or 4b or 4c).
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass mindestens ein Teil des aus der Nachverbrennung (5) ausgetragenen Feststoffes in einem externen Fliessbettkühler (12) unter Wärmerückgewinnung abgekühlt und zurück in die Nachverbrennung geleitet wird.2. The method according to claim 1, characterized in that at least part of the solid discharged from the afterburning (5) is cooled in an external fluid bed cooler (12) with heat recovery and is returned to the afterburning.
3. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die mittlere Suspensionsdichte der Gas-Feststoff¬ mischung in der Wirbelschicht mindestens 50-100 kg/Nm3 beträgt.3. The method according to claim 1, characterized in that the average suspension density of the gas-solid mixture in the fluidized bed is at least 50-100 kg / Nm 3 .
4. Verfahren nach Anspruch 2, dadurch gekennzeichnet, dass die mittlere Suspensionsdichte der Gas-Feststoff¬ mischung in der Wirbelschicht mindestens 20-50 kg/Nm3 beträgt. 4. The method according to claim 2, characterized in that the average suspension density of the gas-solid mixture in the fluidized bed is at least 20-50 kg / Nm 3 .
5. Verfahren nach einem der Ansprüche 1 bis 4, dadu gekennzeichnet, dass Müllkoks als Entgasungsprodu von Innertstoffen befreit und fein gemahlen in d Wirbelschicht mitverbrannt wird.5. The method according to any one of claims 1 to 4, characterized in that waste coke is freed of inert substances as a degassing product and finely ground in the fluidized bed.
6. Verfahren nach einem der Ansprüche 1 bis 5, dadur gekennzeichnet, dass in die Nachverbrennung (4a bz 4b bzw. 4c) zur Stickoxidentfernung Reduktionsmitte vorzugsweise Ammoniak, eingeleitet werden.6. The method according to any one of claims 1 to 5, characterized in that in the afterburning (4a or 4b or 4c) for the removal of nitrogen oxide, reducing agents, preferably ammonia, are introduced.
7. Verfahren nach einem der Ansprüche 1 bis 5, dadur gekennzeichnet, dass bei der Entfernung der Feststof (8) nach der Nachverbrennung zur Stickoxidentfernu Reduktionsmittel, vorzugsweise Ammoniak, eingeleit werden.7. The method according to any one of claims 1 to 5, characterized in that the removal of the solids (8) after the afterburning for nitrogen oxide removal reducing agents, preferably ammonia, are initiated.
8. Vorrichtung zum Durchführen des Verfahrens na Anspruch 1, mit einer Pyrolysekammer (2) und einer die Pyrolysekammer (2) angeschlossenen Nachbrennkamm (4a bzw. 4b bzw. 4c), dadurch gekennzeichnet, dass d Nachbrennkammer (4a bzw. 4b bzw. 4c) als e Wirbelschichtreaktor ausgebildet ist, dem ein Stau abscheider (8) nachgeschaltet ist, wobei eine Rüc verbindung (9) des Staubabscheiders (8) mit d Nachbrennkammer (4a bzw. 4b bzw. 4c) vorhanden ist z Rezirkulieren des im Staubabscheider (9) abgeschi denen Feststoffes.8. Apparatus for performing the method according to claim 1, with a pyrolysis chamber (2) and an afterburning comb (4a or 4b or 4c) connected to the pyrolysis chamber (2), characterized in that d afterburning chamber (4a or 4b or 4c ) is designed as an e fluidized bed reactor, which is followed by a trap separator (8), a back connection (9) of the dust separator (8) with d afterburner chamber (4a or 4b or 4c) being present for recirculating the dust separator (9 ) separated solids.
9. Vorrichtung nach Anspruch 8, dadurch gekennzeichne dass die Wände des Wirbelschichtreaktors als Wärm übertragungsflächen (6) ausgestaltet sind.9. The device according to claim 8, characterized in that the walls of the fluidized bed reactor are designed as heat transfer surfaces (6).
10. Vorrichtung nach einemder Ansprüche 8 bis 9, dadur gekennzeichnet, dass zum Rezirkulieren des im Stau abscheider (8) abgeschiedenen Feststoffes eine üb einen externen Fliessbetkuhler (12) zur Nachbrenn¬ kammer (4b bzw. 4c) führende Rückverbindung (13,14) vorhanden ist. 10. The device according to one of claims 8 to 9, characterized in that for the recirculation of the solid separated in the jam separator (8) separated over a there is an external fluid bed cooler (12) leading back connection (13, 14) to the afterburning chamber (4b or 4c).
EP96900074A 1995-01-10 1996-01-08 Process for the heat treatment of waste material Expired - Lifetime EP0749551B1 (en)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
CH00053/95A CH690790A5 (en) 1995-01-10 1995-01-10 A process for the thermal treatment of waste material.
CH53/95 1995-01-10
CH5395 1995-01-10
PCT/CH1996/000007 WO1996021824A1 (en) 1995-01-10 1996-01-08 Process for the heat treatment of waste material

Publications (2)

Publication Number Publication Date
EP0749551A1 true EP0749551A1 (en) 1996-12-27
EP0749551B1 EP0749551B1 (en) 2000-04-05

Family

ID=4178248

Family Applications (1)

Application Number Title Priority Date Filing Date
EP96900074A Expired - Lifetime EP0749551B1 (en) 1995-01-10 1996-01-08 Process for the heat treatment of waste material

Country Status (13)

Country Link
US (1) US5915311A (en)
EP (1) EP0749551B1 (en)
JP (1) JPH09506424A (en)
AT (1) ATE191551T1 (en)
CA (1) CA2184102A1 (en)
CH (1) CH690790A5 (en)
CZ (1) CZ285991B6 (en)
DE (1) DE59604863D1 (en)
FI (1) FI963526A (en)
NO (1) NO963773L (en)
NZ (1) NZ300141A (en)
PL (1) PL316148A1 (en)
WO (1) WO1996021824A1 (en)

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6276306B1 (en) * 2000-08-03 2001-08-21 Michael L. Murphy Apparatus for recovering hydrocarbons from granular solids
US9127208B2 (en) 2006-04-03 2015-09-08 Pharmatherm Chemicals, Inc. Thermal extraction method and product
US7905990B2 (en) * 2007-11-20 2011-03-15 Ensyn Renewables, Inc. Rapid thermal conversion of biomass
US20090151609A1 (en) * 2007-12-15 2009-06-18 Hoskinson Gordon H Incinerator with pivoting grating system
US20110284359A1 (en) 2010-05-20 2011-11-24 Uop Llc Processes for controlling afterburn in a reheater and for controlling loss of entrained solid particles in combustion product flue gas
US8499702B2 (en) 2010-07-15 2013-08-06 Ensyn Renewables, Inc. Char-handling processes in a pyrolysis system
US9441887B2 (en) 2011-02-22 2016-09-13 Ensyn Renewables, Inc. Heat removal and recovery in biomass pyrolysis
US9347005B2 (en) 2011-09-13 2016-05-24 Ensyn Renewables, Inc. Methods and apparatuses for rapid thermal processing of carbonaceous material
US10400175B2 (en) 2011-09-22 2019-09-03 Ensyn Renewables, Inc. Apparatuses and methods for controlling heat for rapid thermal processing of carbonaceous material
US9109177B2 (en) 2011-12-12 2015-08-18 Ensyn Renewables, Inc. Systems and methods for renewable fuel
US9670413B2 (en) 2012-06-28 2017-06-06 Ensyn Renewables, Inc. Methods and apparatuses for thermally converting biomass
TWI645026B (en) 2013-06-26 2018-12-21 安信再生公司 Systems and methods for renewable fuel
CA2995845A1 (en) 2015-08-21 2017-03-02 Ensyn Renewables, Inc. Liquid biomass heating system
CA3048681A1 (en) 2016-12-29 2018-07-05 Ensyn Renewables, Inc. Demetallization of liquid biomass

Family Cites Families (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS50133995A (en) * 1974-04-11 1975-10-23
US4325327A (en) * 1981-02-23 1982-04-20 Combustion Engineering, Inc. Hybrid fluidized bed combuster
DE3113993A1 (en) * 1981-04-07 1982-11-11 Metallgesellschaft Ag, 6000 Frankfurt METHOD FOR THE SIMULTANEOUS PRODUCTION OF COMBUSTION GAS AND PROCESS HEAT FROM CARBON-MATERIAL MATERIALS
DE3307848A1 (en) * 1983-03-05 1984-09-06 Metallgesellschaft Ag, 6000 Frankfurt METHOD FOR REBURNING AND PURIFYING PROCESS EXHAUST GAS
DE3310534A1 (en) * 1983-03-23 1984-10-04 C. Deilmann AG, 4444 Bad Bentheim DEVICE FOR RECOVERING ENERGY FROM PYROLIZABLE, CARBONATED WASTE MATERIALS, ALTERNATING COMPOSITION
US4602573A (en) * 1985-02-22 1986-07-29 Combustion Engineering, Inc. Integrated process for gasifying and combusting a carbonaceous fuel
JPH0341729A (en) * 1989-07-07 1991-02-22 Tokyo Electron Ltd Substrate cleaning
DE4112593C2 (en) * 1991-04-17 1995-03-23 Pka Umwelttech Gmbh & Co Kg Process and plant for the thermal treatment of metal scrap contaminated with organic components
US5347953A (en) * 1991-06-03 1994-09-20 Foster Wheeler Energy Corporation Fluidized bed combustion method utilizing fine and coarse sorbent feed
AU1449992A (en) * 1992-03-05 1993-10-05 Technische Universiteit Delft Method and apparatus for combusting a carbonaceous material
CZ289723B6 (en) * 1992-06-28 2002-03-13 Ormat Industries Ltd. Process for preparing combustible gases from solid fuel and apparatus for making the same
US5379705A (en) * 1992-11-11 1995-01-10 Kawasaki Jukogyo Kabushiki Kaisha Fluidized-bed incinerator
FR2701087B1 (en) * 1993-02-04 1999-08-06 Tiru Process for the incineration of solid fuels, in particular urban residues, with solid and gaseous discharges which are substantially neutral vis-à-vis the environment.
FI933961A (en) * 1993-06-24 1994-12-25 Ahlstroem Oy Method for treating solids at high temperature
DE4327953A1 (en) * 1993-08-19 1995-02-23 Siemens Ag Plant for thermal waste disposal and method for operating such a plant

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO9621824A1 *

Also Published As

Publication number Publication date
PL316148A1 (en) 1996-12-23
US5915311A (en) 1999-06-29
ATE191551T1 (en) 2000-04-15
NO963773D0 (en) 1996-09-09
EP0749551B1 (en) 2000-04-05
DE59604863D1 (en) 2000-05-11
CH690790A5 (en) 2001-01-15
JPH09506424A (en) 1997-06-24
CZ285991B6 (en) 1999-12-15
NO963773L (en) 1996-11-11
FI963526A0 (en) 1996-09-09
CZ259296A3 (en) 1997-02-12
CA2184102A1 (en) 1996-07-18
NZ300141A (en) 1997-10-24
WO1996021824A1 (en) 1996-07-18
FI963526A (en) 1996-09-09

Similar Documents

Publication Publication Date Title
EP1192234B1 (en) Method and device for pyrolyzing and gasifying organic substances or substance mixtures
EP1226222B1 (en) Method for gasifying organic materials and mixtures of materials
EP0118931B1 (en) Afterburning and cleaning proces of off-gases
EP0749551B1 (en) Process for the heat treatment of waste material
DE2624302A1 (en) PROCEDURE FOR CARRYING OUT EXOTHERMAL PROCESSES
DE4109136C2 (en) Method and device for processing contaminated waste
DE1909263A1 (en) Method and device for smoldering fine-grained bituminous substances which form a dust-like smoldering residue
EP1187891B1 (en) Method and device for disposing of waste products
EP1201731A1 (en) Process for fluidized bed gasifying carbon containing solids and gasifier therefor
EP0862019B1 (en) Method and device for thermal treatment of fly ash from grate incinerators
WO2001057161A1 (en) 2-stage cooling process for synthesis gas
DE3023670C2 (en) Method and device for smoldering oil shale
DE2508707A1 (en) PROCESS FOR DEFLATING BITUMINOESE OR OILY MATERIAL
DE4226015C1 (en) Process for the disposal of solid and liquid waste in the gasification process in fixed bed pressure gasification
DE102007030394A1 (en) Thermal treatment of sulfide ores such as molybdenite to produce molybdenum trioxide, by roasting enriched ore concentrate in first reactor, separating the solids in separator, and converting the solid to metallic oxide in second reactor
EP0215210B1 (en) Process and installation for preparing binder-free hot-briquets
EP0749553B1 (en) Method of burning waste material to recover thermal energy
DE4425117C2 (en) Process for the combustion of sewage sludge in a fluidized bed boiler
EP0704658A2 (en) Process for thermal treatment of waste material, especially refuse, and rotary drum furnace for carrying out the process
DD252617A5 (en) METHOD FOR USING THE IRON CONTENT OF IRON ORES, OXYGENIC SUBSTANCES, AND BY-PRODUCTS AND WASTE IRON AND STEEL INDUSTRY WASTE
EP0040857B1 (en) Process and apparatus for the separation of gaseous and solid noxious products from residues arising from thermal processes, particularly from the pyrolysis of refuse
WO2001010977A1 (en) Method of evaluating gas from a sedimentation basin
EP0089075B1 (en) Method of burning the combustible constituents in the waste gases of rotary furnaces
DE2637427B2 (en) Process for heating fine-grained carbonaceous material
EP0504502A1 (en) Process and apparatus for the treatment of waste containing noxious substances

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 19960816

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FR GB IT LI LU NL SE

17Q First examination report despatched

Effective date: 19981013

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

ITF It: translation for a ep patent filed

Owner name: BARZANO' E ZANARDO MILANO S.P.A.

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE CH DE DK ES FR GB IT LI LU NL SE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20000405

Ref country code: ES

Free format text: THE PATENT HAS BEEN ANNULLED BY A DECISION OF A NATIONAL AUTHORITY

Effective date: 20000405

REF Corresponds to:

Ref document number: 191551

Country of ref document: AT

Date of ref document: 20000415

Kind code of ref document: T

REG Reference to a national code

Ref country code: CH

Ref legal event code: NV

Representative=s name: PATENTANWAELTE SCHAAD, BALASS, MENZL & PARTNER AG

Ref country code: CH

Ref legal event code: EP

REF Corresponds to:

Ref document number: 59604863

Country of ref document: DE

Date of ref document: 20000511

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20000705

ET Fr: translation filed
GBV Gb: ep patent (uk) treated as always having been void in accordance with gb section 77(7)/1977 [no translation filed]

Effective date: 20000405

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010108

Ref country code: AT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010108

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010131

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
BERE Be: lapsed

Owner name: VON ROLL UMWELTTECHNIK A.G.

Effective date: 20010131

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20050110

Year of fee payment: 10

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 20050111

Year of fee payment: 10

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20060109

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20060112

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20060113

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: CH

Payment date: 20060119

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20060131

Year of fee payment: 11

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20060801

EUG Se: european patent has lapsed
NLV4 Nl: lapsed or anulled due to non-payment of the annual fee

Effective date: 20060801

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20070131

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20070131

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20070801

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

Effective date: 20070930

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20070131

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20070108