EP0524847A1 - Verfahren und Vorrichtung zur Abfallbehandlung durch direkten Kontakt - Google Patents

Verfahren und Vorrichtung zur Abfallbehandlung durch direkten Kontakt Download PDF

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Publication number
EP0524847A1
EP0524847A1 EP92401828A EP92401828A EP0524847A1 EP 0524847 A1 EP0524847 A1 EP 0524847A1 EP 92401828 A EP92401828 A EP 92401828A EP 92401828 A EP92401828 A EP 92401828A EP 0524847 A1 EP0524847 A1 EP 0524847A1
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EP
European Patent Office
Prior art keywords
thermolysis
gases
waste
hot
industrial
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
EP92401828A
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English (en)
French (fr)
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EP0524847B1 (de
Inventor
Gérard Martin
Robert Gaulard
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.)
THIDE ENVIRONNEMENT
IFP Energies Nouvelles IFPEN
Original Assignee
THIDE ENVIRONNEMENT
IFP Energies Nouvelles IFPEN
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Publication date
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Publication of EP0524847A1 publication Critical patent/EP0524847A1/de
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Publication of EP0524847B1 publication Critical patent/EP0524847B1/de
Anticipated expiration legal-status Critical
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    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/06—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated according to the moving bed type
    • 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
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/02—Treating solid fuels to improve their combustion by chemical means

Definitions

  • the present invention relates to the treatment of industrial and / or household waste and more specifically their thermolysis.
  • the Applicant has presented in its patent application EN 90.13844 a process and an installation comprising a thermolysis operation of the waste followed by a hot and dry treatment of the effluents resulting from the pyrolysis.
  • the main purpose of this implementation is to reduce or even eliminate most of the pollutants present in the pyrolysis effluents and usually discharged into the atmosphere.
  • the document DE-35.09.275 discloses a process for the treatment of household residues according to which these residues are successively dried, heated and then cooled, the gases resulting from combustion being able to be treated and then partially discharged into the atmosphere partly recycled.
  • thermolysis In terms of the treatment of solids from thermolysis, the Applicant has also disclosed a treatment of waste by thermolysis comprising dechlorination by washing said solids.
  • This implementation has in particular the advantage of producing a coke free of most of the pollutants, that is to say an easily reusable coke, having an improved calorific value with respect to systems which do not treat the solid products from thermolysis.
  • the present invention aims to improve the thermolysis of industrial waste by proposing not only to perform dechlorination of the solids resulting from thermolysis but also by directly heating, by contacting in the pyrolysis means, the waste with hot heat-carrying gases.
  • thermolysis a process for treating industrial and / or household waste comprising in particular a drying step, a step of thermolysis of the waste, and a step of dechlorination by washing the solids resulting from the thermolysis.
  • thermolysis is carried out by direct contact of the waste with hot gases having a low oxygen content.
  • the oxygen content of hot gases used for thermolysis is less than 10%, preferably less than 4% by volume.
  • the hot gases used for thermolysis can essentially consist of recycled thermolysis gases.
  • the contact takes place against the current in the thermolysis means.
  • the hot gases used for thermolysis essentially consist of effluents from combustion in a fluidized bed, the oxygen content of which is controlled.
  • thermolysis a fraction of the gases resulting from thermolysis pass through a heat exchanger before being recycled as heat transfer gas.
  • the hot gases used for the drying step come either from a specific generator, or from a heat exchanger supplied with the gases from said specific generator.
  • thermolysis means comprises at least one inlet for the waste and at least one inlet for hot gases, the waste and the hot gases being in direct contact in the thermolysis means.
  • the means for generating hot smoke can consist of a reactor operating in a fluidized bed.
  • the installation can also include at least one preheating exchanger placed for example at the inlet of the thermolysis means.
  • the installation can also include a second heat exchanger, between the gases from the means for generating hot smoke and the air supplying a dryer.
  • FIG. 1 is shown schematically a preferred embodiment of the invention, according to which the installation essentially comprises a drying enclosure 1 crossed both by the waste to be treated (line 2) and by hot gases brought in by the line 3.
  • the hot gases enter the dryer 1 at a temperature between 200 and 1200 ° C, preferably between 400 and 800 ° C. They emerge from it, through line 9, at a temperature between 50 and 100 ° C.
  • the dryer 1 operates cocurrently (the waste and the hot gases move in the same direction) in order to avoid the risks of ignition of the waste.
  • thermolysis reactor (or means) 4 which, according to the invention, operates in a vertical moving bed.
  • the waste is introduced into the upper part of the thermolysis reactor 4 and passes by gravity into the reactor with a substantially vertical axis.
  • the hot gases are preferably introduced at the base (or near the base) of the reactor 4 by any device known per se 6. The hot gases percolate in ascending current through the waste bed and they gradually transfer their energy to solid.
  • the temperature of the waste gradually increases as it migrates down from the reactor 4, finally reaching the temperature of the hot gases before their introduction into the reactor 4, ie a temperature of between 300 ° C. and 1000 ° C and preferably between 400 and 600 ° C.
  • the hot solids essentially made up of coke and mineral matter, are evacuated from the reactor 4 by the line 7 located at the bottom of the reactor 4.
  • the reactor 4 therefore operates in a moving bed against the current (possibly in a fluidized bed at the location thermolyser where the particle size is small.
  • the condensation water from the drying effluents, supplied by a line 11, is preferably used for this operation.
  • This condensation water can come from a condenser 8 supplied by the wet gases coming from the dryer 1 via a line 9.
  • thermolysis reactor 4 A mixing between the solids from the thermolysis reactor 4 and the abovementioned washing waters is therefore carried out in enclosure 10.
  • the mixture is intended to essentially remove the chlorides present in the solids from reactor 4.
  • the mixture is then evacuated to a means 12 intended to separate the solids which have been freed from the chlorides of the washing water:
  • the depolluted solids are extracted by line 14 while the washing water is extracted by a specific line 13.
  • the washing water is preferably filtered (filter not shown) before being returned via line 13 to the condenser 8. This reuse of the washing water is in no way obligatory. However, it is useful if only in terms of the savings achieved.
  • the heating gases circulate against the current of the waste, that is to say from bottom to top in the reactor 4.
  • These heating gases are accompanied by gases generated by thermolysis, so that the mass flow rate of outgoing gas is greater. than the mass flow of incoming gas.
  • a fan 16 in any other means for setting in motion the gaseous mixture can be placed at the outlet of the reheating means 15 in order to ensure the circulation of said mixture.
  • This mixing is however not mandatory for the implementation of the invention.
  • thermolysis gases is then sent via a line 251 to a gas-gas heat exchanger 17 in order to be reheated again, before entering the reactor 4 via line 18.
  • the gases are commonly brought to a temperature between 300 and 1000 ° C., preferably between 400 and 600 ° C.
  • the flow rate and the final temperature of the thermolysis gases thus recycled can be continuously adjusted in order to compensate for any thermal losses in the thermolysis reactor 4, and in order to provide the energy necessary for thermolysis.
  • the temperature of the gases at the level of line 18 is also fixed taking into account the fouling problems which may arise if the gases crack inside the exchanger 17.
  • thermolysis gases heated in the means 15 and then ventilated, can be sent to a specific generator 19.
  • This generator 19 is therefore used to burn said thermolysis gases.
  • the generator 19 is also used to incinerate any traces of organic matter present in the drying effluents. These are brought by one or more specific line (s) 20.
  • the temperature of the gases is of the order of 800 to 1600 ° C.
  • a part of the gases from the generator 19 is used to supply the dryer 1 with hot gases via a line 21 and then via the line 3.
  • the other part of these gases is sent via a line 22 to the gas-gas exchanger 17.
  • thermolysis gases therefore serve to preheat the recycled part of the thermolysis gases.
  • FIG. 2 shows a second embodiment of the invention which differs from that which has just been described only by the means intended to burn the gases resulting from thermolysis.
  • FIG. 2 shows only the modified part of the installation and only this part of the installation and its operation will be described in detail below.
  • a fluidized bed 40 is used to burn the thermolysis gases.
  • thermolysis gases we will choose to use a fluidized bed in some cases especially when the calorific value of the thermolysis gases is low or is variable over time.
  • the fluidized bed thanks to its high thermal inertia, ensures stable combustion even when the calorific value of the gases to be burned drops significantly.
  • thermolysis gases once reheated in the means 15 and set in motion in the means 16, are then directed to the reactor 40 operating in a fluidized bed.
  • thermolysis gases are distributed by a device 41 while the combustion air is introduced by a line 42 preferably located at the bottom of the reactor 40.
  • a line 42 preferably located at the bottom of the reactor 40.
  • Any means 43 known per se can be used to distribute the combustion air.
  • the combustion air will preferably be preheated, for example by means of a gas-gas exchanger 44 in which a part of the hot gases extracted from the reactor 40 also circulates via a line 45.
  • the quantity of combustion air introduced into the reactor 40 is adjusted so as to permanently maintain a low oxygen content for the thermolysis gases. Indeed, part of the fumes produced by the reactor 40 is directed via a line 46 to the reactor 4 for thermolysis of the waste (the other part serving to preheat the combustion air as already mentioned).
  • thermolysis gases The control of the oxygen content of the thermolysis gases is indeed very important for the proper conduct of the process according to the invention. This control can be carried out using a control loop (not shown in Figure 2).
  • the fluidized fit 40 operates at a temperature between 700 and 1300 ° C, preferably between 800 and 1000 ° C.
  • the reactor 40 can operate with gases having low calorific values, less than 1500 KJ / Nm3.
  • the fluidized bed 40 is formed wholly or partly by calcium agents such as lime or limestones, traces of hydrochloric acid, hydrofluoric acid or sulphates, not captured in the thermolysis reactor 4, can be easily trapped at reactor 40 by these calcium substances.
  • Another scenario can arise when the waste to be treated has a very high humidity.
  • FIG. 3 shows an example of installation that can be envisaged in this scenario.
  • the elements common to the embodiments already described keep the same references as in the previous figures and will not be described again. Only the elements specific to this embodiment will now be defined.
  • the hot gas generator used is preferably a flame incinerator as described in the first embodiment of the invention.
  • the hot gases pass through a first exchanger 50 where they are in contact with the air intended for drying.
  • a line 52 serves to introduce the outside air into the exchanger 50;
  • Line 3 conducts the air heated in the exchanger 50 to the dryer 1.
  • the hot gases enter a second gas-gas exchanger 51 where they are used to heat the part of the thermolysis gases to be recycled.
  • the appropriate pipes (251 and 18) are provided to constitute this recycling circuit which resembles that already defined for the first embodiment of the invention.
  • FIG. 3 The installation shown in FIG. 3 is an illustrative and in no way limitative embodiment of the invention to which a person skilled in the art can make modifications without going beyond the ambit of the invention.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Processing Of Solid Wastes (AREA)
  • Drying Of Solid Materials (AREA)
EP92401828A 1991-07-09 1992-06-26 Verfahren und Vorrichtung zur Abfallbehandlung durch direkten Kontakt Expired - Lifetime EP0524847B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9108717A FR2679009B1 (fr) 1991-07-09 1991-07-09 Procede et dispositif de traitement de dechets par contact direct
FR9108717 1991-07-09

Publications (2)

Publication Number Publication Date
EP0524847A1 true EP0524847A1 (de) 1993-01-27
EP0524847B1 EP0524847B1 (de) 1996-01-24

Family

ID=9414966

Family Applications (1)

Application Number Title Priority Date Filing Date
EP92401828A Expired - Lifetime EP0524847B1 (de) 1991-07-09 1992-06-26 Verfahren und Vorrichtung zur Abfallbehandlung durch direkten Kontakt

Country Status (7)

Country Link
US (2) US5505822A (de)
EP (1) EP0524847B1 (de)
AT (1) ATE133445T1 (de)
DE (1) DE69207836T2 (de)
ES (1) ES2086096T3 (de)
FR (1) FR2679009B1 (de)
GR (1) GR3018833T3 (de)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0593911A1 (de) * 1992-09-26 1994-04-27 RWE Entsorgung Aktiengesellschaft Verfahren zum beschleunigten thermischen Spalten synthetischer organischer Abfälle
FR2701035A1 (fr) * 1993-02-01 1994-08-05 Thermolyse Ste Francaise Procédé et installation pour le traitement par thermolyse de déchets solides, sans condensation d'hydrocarbures.
FR2754539A1 (fr) * 1996-10-15 1998-04-17 Thermolyse Soc France Procede de traitement de dechets par injection de gaz chauds directement dans la charge a traiter, installation et chariot pour la mise en oeuvre de ce procede
FR2754540A1 (fr) * 1996-10-15 1998-04-17 Thermolyse Soc France Procede et installation pour le traitement de dechets solides par thermolyse
WO1998016594A1 (fr) * 1996-10-15 1998-04-23 Societe Française De Thermolyse Installation de traitement de déchets par injection de gaz chauds dans la charge à traiter et recyclage des gaz de thermolyse produits
EP3854861A1 (de) * 2020-01-22 2021-07-28 Slb Sarl Verfahren und anlage zur produktion von bio-kohle und ähnlichen produkten

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2722436B1 (fr) 1994-07-13 1996-09-20 Inst Francais Du Petrole Procede et installation de thermolyse de dechets
FR2735707A1 (fr) 1995-06-20 1996-12-27 Minghi Osvald Procede et dispositif de rehabilitation de matieres et sols pollues en continu par pyrolyse sous atmosphere controlee
US20060163053A1 (en) * 2005-01-21 2006-07-27 Bengt-Sture Ershag Batch pyrolysis system
US20090114519A1 (en) * 2006-04-03 2009-05-07 Recuperacion Materiales Diversos, S.A. Process and Equipment for the Treatment of Waste Materials

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2331752A1 (fr) * 1975-11-13 1977-06-10 Picard Du Chambon Michel Unite de traitement des residus menagers et professionnels par decomposition thermique dite pyrolyse
GB2106934A (en) * 1981-09-19 1983-04-20 Coal Ind Method of dechlorinating coal
DE3509275A1 (de) * 1984-03-23 1985-12-19 Carl Still Gmbh & Co Kg, 4350 Recklinghausen Verfahren zur thermischen behandlung von waschbergen
EP0426925A1 (de) * 1989-11-07 1991-05-15 Societe Anonyme Dite: C.G.C. Entreprise Verfahren und Anlage zur Behandlung von städtischen und industriellen AbfÀ¤llen

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DE1935214A1 (de) * 1969-07-11 1971-01-14 Metallgesellschaft Ag Verfahren und Vorrichtung zur Erzeugung von feinkoernigem Koks
US3862887A (en) * 1971-12-22 1975-01-28 Monsanto Enviro Chem Syst Method for processing heat-decomposable non-gaseous materials
DE2244753B1 (de) * 1972-09-08 1973-10-18 Mannesmann Ag, 4000 Duesseldorf Verfahren und Vorrichtung zur Ver mchtung von Mull
GB1485760A (en) * 1973-09-07 1977-09-14 Nat Res Dev Pyrolysis of domestic and other waste
US3926045A (en) * 1974-01-30 1975-12-16 Nartron Corp Flow sensor and system
JPS523644A (en) * 1975-06-25 1977-01-12 Teijin Ltd Process for manufacturing hollow molded articles
US4050991A (en) * 1976-04-23 1977-09-27 Kautz Walter C Jr Pyrolytic reducer and condenser apparatus
US4303477A (en) * 1979-06-25 1981-12-01 Babcock Krauss-Maffei Industrieanlagen Gmbh Process for the pyrolysis of waste materials
DE3069079D1 (en) * 1979-11-25 1984-10-04 Ofag Ofenbau Feuerungstech Ag Process for producing carbon-enriched solid products and matching use of a kiln installation
JPS591758B2 (ja) * 1980-01-18 1984-01-13 工業技術院長 熱分解装置のガス処理方法
DE3040227C2 (de) * 1980-10-24 1984-03-29 Deutsche Kommunal-Anlagen Miete GmbH, 8000 München Verfahren zur Weiterverarbeitung von aus heizwertreichen Abfällen durch thermische Behandlung erhaltener Pyrolysegase

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2331752A1 (fr) * 1975-11-13 1977-06-10 Picard Du Chambon Michel Unite de traitement des residus menagers et professionnels par decomposition thermique dite pyrolyse
GB2106934A (en) * 1981-09-19 1983-04-20 Coal Ind Method of dechlorinating coal
DE3509275A1 (de) * 1984-03-23 1985-12-19 Carl Still Gmbh & Co Kg, 4350 Recklinghausen Verfahren zur thermischen behandlung von waschbergen
EP0426925A1 (de) * 1989-11-07 1991-05-15 Societe Anonyme Dite: C.G.C. Entreprise Verfahren und Anlage zur Behandlung von städtischen und industriellen AbfÀ¤llen

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0593911A1 (de) * 1992-09-26 1994-04-27 RWE Entsorgung Aktiengesellschaft Verfahren zum beschleunigten thermischen Spalten synthetischer organischer Abfälle
FR2701035A1 (fr) * 1993-02-01 1994-08-05 Thermolyse Ste Francaise Procédé et installation pour le traitement par thermolyse de déchets solides, sans condensation d'hydrocarbures.
EP0610120A1 (de) * 1993-02-01 1994-08-10 Societe Francaise De Thermolyse Verfahren und Einrichtung für die Thermolyse von festen Abfällen ohne Kondensation von Kohlenwasserstoffen
FR2754539A1 (fr) * 1996-10-15 1998-04-17 Thermolyse Soc France Procede de traitement de dechets par injection de gaz chauds directement dans la charge a traiter, installation et chariot pour la mise en oeuvre de ce procede
FR2754540A1 (fr) * 1996-10-15 1998-04-17 Thermolyse Soc France Procede et installation pour le traitement de dechets solides par thermolyse
WO1998016594A1 (fr) * 1996-10-15 1998-04-23 Societe Française De Thermolyse Installation de traitement de déchets par injection de gaz chauds dans la charge à traiter et recyclage des gaz de thermolyse produits
WO1998016593A1 (fr) * 1996-10-15 1998-04-23 Societe Francaise De Thermolyse Procede et installation pour le traitement de dechets solides par thermolyse
US6168688B1 (en) 1996-10-15 2001-01-02 Societe Francaise De Thermolyse Method and plant for treating solid waste products by thermolysis
EP3854861A1 (de) * 2020-01-22 2021-07-28 Slb Sarl Verfahren und anlage zur produktion von bio-kohle und ähnlichen produkten

Also Published As

Publication number Publication date
ATE133445T1 (de) 1996-02-15
GR3018833T3 (en) 1996-04-30
DE69207836D1 (de) 1996-03-07
US5505822A (en) 1996-04-09
US5616216A (en) 1997-04-01
FR2679009A1 (fr) 1993-01-15
FR2679009B1 (fr) 1997-12-12
ES2086096T3 (es) 1996-06-16
EP0524847B1 (de) 1996-01-24
DE69207836T2 (de) 1996-05-30

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