EP0908673B1 - Procédé de traitement de scories provenants du traitement thermique de déchets - Google Patents

Procédé de traitement de scories provenants du traitement thermique de déchets Download PDF

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Publication number
EP0908673B1
EP0908673B1 EP97810772A EP97810772A EP0908673B1 EP 0908673 B1 EP0908673 B1 EP 0908673B1 EP 97810772 A EP97810772 A EP 97810772A EP 97810772 A EP97810772 A EP 97810772A EP 0908673 B1 EP0908673 B1 EP 0908673B1
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EP
European Patent Office
Prior art keywords
slag
rotary kiln
ash
process according
heavy metals
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.)
Expired - Lifetime
Application number
EP97810772A
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German (de)
English (en)
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EP0908673A1 (fr
Inventor
Bruno Carcer
Hans Rüegg
Christian Steiner
Beat Stoffel
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.)
Alstom SA
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Alstom SA
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 Alstom SA filed Critical Alstom SA
Priority to EP97810772A priority Critical patent/EP0908673B1/fr
Priority to DE59707290T priority patent/DE59707290D1/de
Priority to AT97810772T priority patent/ATE217699T1/de
Priority to TW087116551A priority patent/TW502099B/zh
Priority to US09/169,139 priority patent/US6036484A/en
Priority to KR1019980042446A priority patent/KR19990037010A/ko
Priority to JP10289347A priority patent/JPH11193911A/ja
Priority to NO984755A priority patent/NO984755L/no
Publication of EP0908673A1 publication Critical patent/EP0908673A1/fr
Application granted granted Critical
Publication of EP0908673B1 publication Critical patent/EP0908673B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—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
    • 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
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • F23G5/16—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber
    • 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
    • F23G5/20—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having rotating or oscillating drums
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/30—Solid combustion residues, e.g. bottom or flyash

Definitions

  • the invention relates to the field of thermal waste treatment. she relates to a process for the treatment of slag and / or ash from the thermal treatment of garbage.
  • EP 0 372 039 B1 describes a process for treating the slag from waste incineration plants known in which the slag dry from the incinerator is carried out, a rough cleaning (removing unburned Coarse goods and magnetic parts) is subjected, and then the coarse cleaned slag is separated into at least two fractions and one of them all particles smaller than 2 mm are assigned. This procedure is based on the knowledge that the fine fraction is the largest part of the original contains pollutants contained in the slag. The fine fraction will a special treatment, while the coarse fraction z. B. as a building material suitable is.
  • the volatilization reactions (Reaction of the solid metal oxides with the added carbon to gaseous metals and carbon monoxide) run in the solid layer of the rotary kiln, which is constantly circulated. In the above The volatilization products become gas spaces with an oxidizing atmosphere then reoxidized. These gaseous phase oxidation products are very finely divided so that it is carried away by the flue gas and transported out of the oven and finally separated after the flue gases have cooled down. The low-metal slag is discharged from the furnace, cooled and then opened Dumped.
  • the invention tries the above. Disadvantages with the known preparation of To avoid garbage slag. It is based on the task of being effective and inexpensive Process for the treatment of slag and / or ash from the provide thermal treatment of garbage, which with a robust and simple technology can be realized and with no additional classification and Crushing stages create an inert slag depleted of pollutants.
  • this is the case with a method according to the preamble of the patent claim 1 achieved in that the waste in a first process step is pyrolyzed, gasified or partially incinerated, with slag containing heavy metals and / or ash with a comparatively high carbon content is said slag and / or ash in a second process step in a rotary kiln to a temperature below the melting temperature of the Slag and / or ash is heated up that the slag and / or ash before their discharge from the rotary kiln remains in the rotary kiln for a sufficiently long time, so that the heavy metals contained in it by reduction on the own slag Carbon is converted into its metallic form and the volatile Heavy metals such as zinc, lead, arsenic and cadmium are converted into the gas phase and are discharged from the rotary kiln with the flue gas, and that a heavy metal-depleted slag is discharged from the rotary kiln becomes.
  • the advantages of the invention are that the slag in one of pollutants depleted state arises.
  • the heavy metal contents are clear below the legally stipulated maximum values for inert material dumps of the Swiss Waste Technical Ordinance (TVA) dated 10.12.1990.
  • high Harmful Hydrocarbon compounds, such as. B. dioxins are below the detection limit. Therefore, the slag prepared in this way can be easily Ferrous and non-ferrous metal separation, for example as a building material in the Road construction used or otherwise used. An expensive one Landfill is unnecessary.
  • the preparation means in a rotary kiln the advantageous use of robust technology. Time consuming classification and Crushing stages for processing the slag are not necessary.
  • the slag introduced into the rotary kiln and / or ash contains at least 10% carbon, because then one is sufficient large amount of reducing agent for the reduction and volatilization of heavy metals is available.
  • the slag is dry from the rotary kiln is carried out and separated into at least two fractions, the first Fraction with a particle size larger than approx. 32 mm in a first sieving stage is separated as a screen overflow, and the screen diarrhea of a second classification stage for the purpose of separating the fine fraction 0 ... 2 mm, whereby at least part of the fine fraction 0 ... 2 mm from the slag processing on the Air inlet side is returned to the rotary kiln and burned there. Thereby the ash burnout in the rotary kiln is increased and the pollutant content the slag reduced even more.
  • Rubbish 1 preferably household waste
  • Rubbish 1 is disposed of via a Feeding device, not shown, fed to a waste incinerator 2 and burned there on a grate 3 using the grate firing process.
  • the Incinerator 2 is a boiler 4 and a dedusting system 5 on the gas side, z. B. an electrostatic filter.
  • the incinerator is on the slag side 2 is followed by a rotary kiln 6.
  • the waste 1 is burned in the incinerator 2 with the supply of primary air 7, that a slag 8 is produced which has a loss on ignition of at least 10 % having.
  • the loss on ignition is a measure of the unburned portion in the Slag 8 and thus an indirect measure of the carbon content. So this comparatively high loss on ignition and thus high carbon content is achieved, Incomplete combustion must take place in furnace 2. So far she had Incineration using the grate combustion process is always the goal, if possible the waste 1 to burn completely, i.e. a slag with the lowest possible loss on ignition and thus to generate low carbon content.
  • the heavy metal and carbonaceous slag 8 from the incinerator 2 falls directly from the grate 3 into the rotary kiln 6 without intermediate cooling Discharged dry without water humidification.
  • the slag 8 has after Rust a temperature of approx. 400 ° C.
  • Rust a temperature of approx. 400 ° C.
  • it is together with the filter dust 10 from the dedusting system 5 by means of an oil burner 16 heated to a temperature of 900 ° C. This temperature is below the Melting temperature of the slag / ash 8, 10, but above the volatilization temperature the heavy metals contained therein.
  • the rotary kiln 6 is so large that the Residence time of slag / ash 8, 10 in rotary kiln 6 after heating approx. Is 1.5 hours. For this reason, the rotary tube has a length of 8 m and an inner diameter of 2.5 m.
  • the volatilization reactions (reaction of the heavy metal oxides with that in the Slag containing carbon to gaseous metals and carbon monoxide) run in the solid layer of the rotary kiln 6, which circulates continuously becomes. In the gas space above with an oxidizing atmosphere, the Volatilization products then reoxidized. These reaction products from the gaseous phase are very fine, so that they are entrained by the flue gas 9 become.
  • the flue gas 9 is then cooled in a steam boiler 13 and filtered in a dust filter 14. This filter dust enriched with heavy metals can then be further treated with the aim of being in them recover heavy metals contained.
  • the heavy metal depleted Slag 15 is discharged from the rotary kiln 6, cooled and can after scrapping and non-ferrous metal separation using a magnetic separator or non-metal separator (not shown in Fig. 1) easily used (e.g. as Building materials in road construction) or on a heap.
  • a magnetic separator or non-metal separator not shown in Fig. 1
  • the following table shows for the exemplary embodiment the contents of heavy metals and dioxin for the starting materials and the end product of the rotary kiln 6 compared to the maximum values for inert landfill quality according to TVA: fly ash Slag from rust Slag after rotary kiln TVA, inert landfill quality loss on ignition % 5 > 10.0 ⁇ 1 pb ppm 9000 2500.0 400 500 Zn ppm 16000 4000.0 500 1000 CD ppm 2400 13.0 nn 10 dioxin concentration ng TE / kg 1600 11.5 nn
  • Fig. 2 shows a diagram to clarify what has just been said on the one hand the zinc or lead concentrations in the slag depending on their residence time in the rotary kiln and on the other hand the bed temperatures depending represents from that time.
  • the course of the curves shows that the Schlakke 8 should stay at least one hour in the rotary kiln 6, because only then a sufficiently large depletion of heavy metals takes place.
  • the slag prepared in this way can be used, for example, as a building material in road construction used or otherwise used. An expensive landfill is unnecessary yourself.
  • processing in a rotary kiln is the most advantageous Use of robust technology. Time-consuming classification and shredding stages for the treatment of the slag are not necessary.
  • filter dust 10 can be applied by using only the carbonaceous slag 8 the grate combustion is fed to the rotary kiln 6.
  • waste incineration and slag processing take place in one and the same unit.
  • Untreated domestic waste 1 with a calorific value of approx. 10,000 kJ / kg is introduced into a rotary kiln 6 with a length of 12 m and an inner diameter of 4 m.
  • the amount of waste is 10,000 kg / h.
  • the garbage 1 is now partially burned by the addition of air, the combustion air 7 having been preheated to a temperature of approximately 400 ° C.
  • the amount of combustion air 7 is such that, on the one hand, a temperature of 1000 ° C.
  • the amount of combustion air is 7 12,000 Nm 3 / h.
  • the residence time of the waste 1 in the rotary kiln 6 is approximately 2 hours. This time is sufficient, on the one hand, to burn garbage 1 (incomplete) and, on the other hand, to deplete the resulting slag / ash from heavy metals by volatilizing them.
  • the slag 15 is then discharged from the rotary kiln 6, cooled and, as already described in the first exemplary embodiment, can continue to be used after separation of iron and non-ferrous metal.
  • the flue gas 9 from the rotary kiln 6 is then completely burned out by adding secondary air 11 in the afterburning chamber 12, cooled in the boiler 4 (flue gas amount at the end of the boiler approx. 53 600 Nm 3 / h) and cleaned in a flue gas cleaning system 5.
  • the slag 15 dry from the rotary kiln 6th is carried out and separated into at least two fractions, the first Fraction with a particle size of approx. 32 mm in a first sieving stage is separated as a screen overflow, and the screen diarrhea of a second classification stage for the purpose of separating the fine fraction 0 ... 2 mm, and at least part of the fine fraction 0 ... 2 mm from the slag processing on the Air inlet side is returned to the rotary kiln 6 and burned there. Thereby the ash burnout in the rotary kiln 6 is increased and the pollutant content the slag further reduced.

Claims (10)

  1. Procédé de préparation de scorie et/ou de cendre en provenance du traitement thermique d'ordures, caractérisé en ce que les ordures (1) sont pyrolysées, gazéifiées ou partiellement brûlées dans une première étape de procédé, une scorie et/ou une cendre (8) contenant des métaux lourds, ayant une teneur relativement élevée en carbone, se formant, en ce que ladite scorie et/ou ladite cendre (8) est échauffée dans une deuxième étape de procédé dans un four tubulaire rotatif (6) à une température en dessous de la température de fusion de la scorie et/ou de la cendre (8), en ce que la scorie et/ou la cendre (8) réside avant son évacuation hors du four tubulaire rotatif (6) pendant une durée suffisamment longue dans le four tubulaire rotatif (6), de telle sorte que les métaux lourds contenus dans cette dernière sont convertis par réduction sur le carbone propre à la scorie en leur forme métallique et que les métaux lourds volatils passent dans la phase gazeuse et sont évacués avec le gaz de fumée (9) hors du four tubulaire rotatif (6), et en ce qu'une scorie appauvrie en métaux lourds (15) est évacuée hors du four tubulaire rotatif (6).
  2. Procédé selon la revendication 1, caractérisé en ce que non seulement la gazéification ou la combustion partielle des ordures (1), mais aussi la réduction et la volatilisation des métaux lourds provenant de la scorie et/ou de la cendre (8) se formant lors de la combustion se font dans une unité unique, c'est-à-dire dans le four tubulaire rotatif (6), la quantité d'air de combustion (7) étant mesurée de telle sorte qu'à l'extrémité du four tubulaire rotatif (6) pratiquement plus d'oxygène ne puisse être détecté.
  3. Procédé selon la revendication 1, caractérisé en ce que la poussière de filtre (10), se formant lors de la pyrolyse, de la gazéification ou de la combustion partielle et déposée dans une installation de dépoussiérage (5), est mélangée à la scorie et/ou la cendre (8) et en ce que celles-ci sont échauffées conjointement dans le four tubulaire rotatif (6) et sont appauvris en métaux lourds.
  4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que le temps de contact de la scorie et/ou la cendre (8) dans le four tubulaire rotatif (6) est supérieur à une heure.
  5. Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que les gaz de fumée (9) provenant du four tubulaire rotatif (6) sont refroidis et dépoussiérés dans un filtre (14).
  6. Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce que la scorie et/ou la cendre (8) sont évacuées à l'état sec sans humidification par l'eau hors du four de pyrolyse ou de combustion (2).
  7. Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que les constituants métalliques résiduels sont éliminés de la scorie (15) évacuée hors du four tubulaire rotatif (6) à l'aide d'un séparateur magnétique et d'un séparateur pour métaux non ferreux.
  8. Procédé selon la revendication 1, caractérisé en ce que la scorie et/ou la cendre (8) introduites dans le four tubulaire rotatif (6) contiennent au moins 10 % de carbone.
  9. Procédé selon la revendication 1, caractérisé en ce que les métaux ferreux et les métaux non ferreux sont séparés de la scorie et/ou la cendre (8) avant leur chargement dans le four tubulaire rotatif (6).
  10. Procédé selon la revendication 1 ou 2, caractérisé en ce que la scorie (15) est évacuée à l'état sec hors du four tubulaire rotatif (6) et est séparée en au moins deux fractions, la première fraction, ayant une grosseur de particule supérieure à environ 32 mm, étant séparée dans une première stade de tamisage en tant que refus de tamisage, et le passant de tamisage d'un deuxième stade de calibrage étant alimenté en vue de la séparation de la partie fine 0... 2 mm, et au moins une partie de la partie fine 0... 2 mm provenant de la préparation de la scorie étant alimentée au côté d'entrée de l'air dans le four tubulaire rotatif (6) et y étant brûlée.
EP97810772A 1997-10-13 1997-10-13 Procédé de traitement de scories provenants du traitement thermique de déchets Expired - Lifetime EP0908673B1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
EP97810772A EP0908673B1 (fr) 1997-10-13 1997-10-13 Procédé de traitement de scories provenants du traitement thermique de déchets
DE59707290T DE59707290D1 (de) 1997-10-13 1997-10-13 Verfahren zur Aufbereitung von Schlacke und/oder Asche aus der thermischen Behandlung von Müll
AT97810772T ATE217699T1 (de) 1997-10-13 1997-10-13 Verfahren zur aufbereitung von schlacke und/oder asche aus der thermischen behandlung von müll
TW087116551A TW502099B (en) 1997-10-13 1998-10-06 Process for reprocessing slag and/or ash from the thermal treatment of refuse
US09/169,139 US6036484A (en) 1997-10-13 1998-10-09 Process for reprocessing slag and/or ash from the thermal treatment of refuse
KR1019980042446A KR19990037010A (ko) 1997-10-13 1998-10-10 폐기물의 열처리로부터 슬래그 및/또는 재를 재처리하는 방법
JP10289347A JPH11193911A (ja) 1997-10-13 1998-10-12 ごみの熱処理からのスラグおよび／または灰の再処理方法
NO984755A NO984755L (no) 1997-10-13 1998-10-12 FremgangsmÕte ved opparbeidelse av slagg og/eller aske fra varmebehandling av avfall

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP97810772A EP0908673B1 (fr) 1997-10-13 1997-10-13 Procédé de traitement de scories provenants du traitement thermique de déchets

Publications (2)

Publication Number Publication Date
EP0908673A1 EP0908673A1 (fr) 1999-04-14
EP0908673B1 true EP0908673B1 (fr) 2002-05-15

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EP97810772A Expired - Lifetime EP0908673B1 (fr) 1997-10-13 1997-10-13 Procédé de traitement de scories provenants du traitement thermique de déchets

Country Status (8)

Country Link
US (1) US6036484A (fr)
EP (1) EP0908673B1 (fr)
JP (1) JPH11193911A (fr)
KR (1) KR19990037010A (fr)
AT (1) ATE217699T1 (fr)
DE (1) DE59707290D1 (fr)
NO (1) NO984755L (fr)
TW (1) TW502099B (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2228146A1 (fr) 2009-03-13 2010-09-15 Kalogeo Anlagenbau GmbH Conditionnement thermique de cendres
EP2428493A1 (fr) 2010-09-08 2012-03-14 Kalogeo Anlagenbau GmbH Traitement thermique de cendre

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DE19961384A1 (de) * 1999-12-20 2001-06-21 Abb Alstom Power Ch Ag Verfahren zur thermischen Behandlung von Rostasche aus Müllverbrennungsanlagen
AU8119801A (en) * 2000-08-10 2002-02-25 Rj Leegroup Inc Low energy method of pyrolysis of hydrocarbon materials such as rubber
KR200314296Y1 (ko) * 2003-03-07 2003-05-23 주식회사 이앤이 감염성 폐기물 소각/ 용융 일체형 처리 시스템
WO2007036914A1 (fr) * 2005-09-30 2007-04-05 Babcock & Wilcox Vølund Aps Chaudiere produisant de la vapeur a partir de gaz de combustion, a haut rendement energetique et qualite amelioree de production de scories
EP2583753B1 (fr) * 2011-10-21 2015-05-13 Enefit Outotec Technology Oü Procédé et appareil de dépoussiérage d'un mélange de gaz et de vapeur
EP2583754B1 (fr) * 2011-10-21 2015-05-13 Enefit Outotec Technology Oü Procédé et appareil d'extraction d'huile d'un mélange de vapeur et gaz
PL2825293T3 (pl) * 2012-03-14 2020-08-24 Mercury Capture Intellectual Property, Llc Sposób obróbki pozostałości węgla aktywnego i węgla ze spalania
EP2992268B1 (fr) * 2013-05-03 2020-01-15 Outotec (Finland) Oy Procédé et installation de séparation de métaux lourds d'un matériau de départ contenant du phosphore
JP6256859B2 (ja) * 2014-02-27 2018-01-10 Ｊｆｅエンジニアリング株式会社 廃棄物焼却方法
RU2653394C1 (ru) * 2017-03-23 2018-05-08 Публичное акционерное общество "Челябинский цинковый завод" Способ переработки цинксодержащих пылей электродуговых печей
CN107101202A (zh) * 2017-04-28 2017-08-29 东南大学 一种降低垃圾焚烧过程中二噁英生成量的处理方法
DE102019107744A1 (de) * 2018-12-20 2020-06-25 Mitsubishi Hitachi Power Systems Europe Gmbh Verfahren und Vorrichtung zur Nachverbrennung von in einer Mono-Klärschlammverbrennungsanlage anfallender Klärschlammasche
AT523447B1 (de) * 2020-02-02 2021-08-15 Alfred Edlinger Dipl Ing Verfahren zum Abtrennen von Phosphor und/oder Phosphorverbindungen aus eisen(oxid)haltigen Phosphor- und/oder Phosphatträgern

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DE2200756A1 (de) * 1972-01-07 1973-07-12 Koppers Wistra Ofenbau Gmbh Verfahren zum gemeinsamen verbrennen von muell und klaerschlamm und einrichtung zur durchfuehrung des verfahrens
JP2857437B2 (ja) 1988-06-16 1999-02-17 アセア・ブラウン・ボベリ・アクチエンゲゼルシヤフト 廃棄物燃焼炉から出たスラグの調製方法及びその装置
ATE173332T1 (de) 1992-02-26 1998-11-15 Hans Kuenstler Verfahren zum einschmelzen von verbrennungsrückständen in schlacke
FR2689617B1 (fr) * 1992-04-02 1994-07-01 Vanderpol Jean Pierre Procede et dispositif pour le traitement thermique de dechets, notamment solides, contenant des matieres organiques.
TW277101B (en) 1995-01-21 1996-06-01 Abb Man Ag Process for treating slag from refuse incineration plants

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2228146A1 (fr) 2009-03-13 2010-09-15 Kalogeo Anlagenbau GmbH Conditionnement thermique de cendres
EP2428493A1 (fr) 2010-09-08 2012-03-14 Kalogeo Anlagenbau GmbH Traitement thermique de cendre

Also Published As

Publication number Publication date
NO984755D0 (no) 1998-10-12
US6036484A (en) 2000-03-14
NO984755L (no) 1999-04-14
JPH11193911A (ja) 1999-07-21
EP0908673A1 (fr) 1999-04-14
ATE217699T1 (de) 2002-06-15
DE59707290D1 (de) 2002-06-20
TW502099B (en) 2002-09-11
KR19990037010A (ko) 1999-05-25

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