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WO1988004013A1 - Procede de purification de gaz de fumee - Google Patents

Procede de purification de gaz de fumee Download PDF

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Publication number
WO1988004013A1
WO1988004013A1 PCT/DK1987/000141 DK8700141W WO8804013A1 WO 1988004013 A1 WO1988004013 A1 WO 1988004013A1 DK 8700141 W DK8700141 W DK 8700141W WO 8804013 A1 WO8804013 A1 WO 8804013A1
Authority
WO
WIPO (PCT)
Prior art keywords
flue gas
combustion
furnace
waste
dewpoint
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.)
Ceased
Application number
PCT/DK1987/000141
Other languages
English (en)
Inventor
Hans Erik Hempel Hansen
Mogens Vinzentz Jensen
Ejler Lautrup Holm
Hanne Færch MADSEN
Jens Peter Sandemand
Carsten Nielsen
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.)
Hj Hansen Holding AS
Aalborg Vaerft AS
Original Assignee
Hj Hansen Holding AS
Aalborg Vaerft AS
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
Priority claimed from DK548786A external-priority patent/DK548786A/da
Application filed by Hj Hansen Holding AS, Aalborg Vaerft AS filed Critical Hj Hansen Holding AS
Publication of WO1988004013A1 publication Critical patent/WO1988004013A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound

Definitions

  • the present invention relates to a process for purification of flue gas from waste combustion in a furnace under fluid-bed conditions.
  • shredder waste Another problematic waste material turns up in connection with the scrapping of old cars arid other sandwich structures containing iron and metal.
  • a mechanical fragmentation plant normally called a shredder plant
  • the cars are smashed, whereafter a sorting of the produced mate ⁇ rial consisting of large and small parts or particles, takes place.
  • mate ⁇ rial consisting of large and small parts or particles
  • shredder waste Another fraction from the sorting, called shredder waste, consists mainly of plastic, rubber, textile fibres, wood, glas, paint remainders, metals and metal oxides.
  • shredder waste represents energy of about 15000 kJ/kg, and today when Europe alone produces more than 1 million tons of shredder waste annually, it is easily understood that it would mean an enormous progress, if shredder waste could be eliminated in an environ ⁇ mentally defendable manner simultaneously with exploitation of the energy.
  • combustion under fluid-bed conditions may be used for many types of solids containing large, heavy and/or irregularly shaped foreign bodies and other non-inflammable components, such as metal, cf. US patent specification No. 4,576,102 and US patent specifi ⁇ cation No. 4,553,487.
  • combustion under slow fluidization conditions in a so-called bubble bed will be suited for this kind of materials, because the relatively long residence time creates a possibi ⁇ lity for good contact between the combustion air and the particles to be combusted.
  • known methods for fluid-bed combustion such as the one mentioned above, may only be used ⁇ for combustion of the types of waste discussed above, if an efficient purification of the flue gas is provided.
  • the present invention is based on the observation that by combus ⁇ tion of the waste materials mentioned a considerable part of the pol ⁇ luting components of the flue gas may be deposited by a cooling of the flue gas, including oxides, in particular metal oxides pertaining typi ⁇ cally from combustion of light metals such as aluminum and magnesium.
  • Other polluting components will be acid gas components, such as S0 2 , SO,, HF and above all HC1.
  • the invention aims at removing to the greatest possible extent the polluting components from the flue gas as solids and this in a manner where these solids are sepa ⁇ rated in fractions which may be individually deposited or, best, reused.
  • Another essential aspect of the invention aims at utilizing the energy content of the waste by extracting as much energy as possible from the flue gas for the production of heat, electricity or combined power/heat.
  • the process of the invention is characterized in that the hot flue gas generated by the combustion, in the furnace or in a flue gas channel connected therewith is brought into contact with a cooled inner surface in such a manner that coatings are formed thereon and that these coatings are removed from the surface.
  • the coatings will consist of the components of the flue gas which may be deposited by the chosen cooling method. If lime or another alkaline absorption agent has not been added to the furnace, the above mentioned acid components will therefore not precipitate, but may be removed at a later time as will be explained in more detail below.
  • the combustion is preferably performed at a temperature of 750-1200°C, this being con ⁇ trolled by a suitable choice of the combustion parameters, in particular the velocity and pressure of the combustion air.
  • a relatively low combustion temperature of 900-1000° C. is preferred in order to avoid to the greatest possible extent that the metal content melts, as would be the case by combustion in a traditional furnace.
  • Components of the waste material, which are oxidizable or inflammable at the prevailing combustion parameters, are carried along by the flue gas and deposited on the cooled inner surface in question.
  • the waste material is mainly non-metallic shredder waste according to a preferred embodiment of the invention, the deposited coating will therefore consist of or contain metal oxides.
  • sand or a similar fluidization material be brought to the fluid bed of the furnace.
  • the fluidized bed is preferably of a slow or bubbling type, sand particles will to a certain extent be carried along by the flue gas, just as a certain amount of sand particles will be removed from the bot ⁇ tom of the combustion chamber together with non-inflammable waste compo ⁇ nents, e.g. pieces of metal.
  • the cooled inner surfaces mentioned may have a plane or cylindri- cal (not necessarily circular-cylindrical) shape and the coatings may then be removed by means of a scraping device having a contour corresponding to the shape of the soft curve of the cylindrical sur ⁇ faces, whereby the scraping device may be moved backwards and forwards in the generatrix direction of the cylindrical surface.
  • the scraping device may also be in the form of a rotating brush or another rotating device.
  • the cooled inner surface may also form part of a upright or mainly vertically extending stack, which thus forms part of the flue gas chan ⁇ nel of the furnace.
  • An automatically operating scraping device may then at pre-determined intervals be inserted in the stack through a closable opening at the top, and the loosened coatings may be collected at the bottom of the reaction chamber from where they may be removed at certain moments.
  • said surface forms part of a cooled cyclone.
  • the coatings of e.g. metal oxides deposited on the inner surface of the cyclone are automatically and continuously worn off by the above mentioned entrained particles of sand or like fluidization material.
  • the coating material may therefore together with sand and other solids, e.g. fly ash, at intervals or continuously be removed from the bottom of the cyclone and as desired directed to slag depots or to recirculation in the combustion zone to obtain a better burning out.
  • the cyclone or the otherwise chosen inner surface may be cooled by any suitable medium, e.g. air, but is preferably water cooled in order to thereby create the possibility of the most efficient exploitation of the heat energy content of the flue gas.
  • the flue gas will arrive at the cooled surface at a temperature of the order of 1000°C. and a cooling of the flue gas to about 500°C. will be appropriate.
  • a temperature drop may in prac ⁇ tice be used for heating of district heating water which is fed at a temperature of the order of 75°C.
  • the flue gas is led on, freed from metal oxides and certain other solids, for removal of acid components. Based on a complete combustion in the furnace, the flue gas will at this point typically contain (XL, H ⁇ O, HC1, HF, SO.,, S0 2 , N 2 , C , various nitrogen oxides and fly ash.
  • This flue gas may be purified according to a preferred embodiment of the invention described in more detail in the following.
  • This embodiment is based on the unexpected recognition that a par ⁇ ticularly efficient desulphurization may be obtained by direct addition to the flue gas of a dry, fresh, alkaline absorption agent, if prior to addition of the absorption agent the water dewpoint or temperature of the flue gas is adjusted in such a manner that the actual temperature of the flue gas is only slightly above the water dewpoint of the flue gas, in particular so that the distance between dewpoint temperature and flue gas temperature is 5-50°C, preferably 10-20°C.
  • the alkaline absorption agent is chosen among oxides and hydroxides of calcium, magnesium and the alkali metals and is added in dry form to the flue gas, whereby is meant that it is not a question of a solution, a suspension or another fluid or semi-fluid form, though it is not necessarily an absolutely waterfree product.
  • the preferred absorption agent is a powdered lime hydrate which is in practice about 90% pure Ca(0H) 2 with a small water content of maximum 5%.
  • the required adjustment of the distance to the dewpoint may either be effected by decreasing the temperature of the flue gas or by adding water from the outside or by a combination of both. Since the flue gas as mentioned above typically leaves the cooling cyclone at a temperature of the order of 500°C, it is preferred to perform the dewpoint adjust- ment by passing the flue gas through a heat exchanger, where a cooling to about 55-60°C. typically has the effect that the desired adjustment of the distance to the dewpoint is obtained b the usual, absolute moi ⁇ sture content from a combustion process.
  • this heat exchanger may be shaped as a flue cooler having a convection heat sur- face so that practically the entire content of thermal energy in the flue gas may be utilized.
  • a fresh alkaline absorption agent is as mentioned added in dry form, whereby a quick and willing reaction with the remaining content of S0 2 , and possibly HC1 and HF, of the flue gas takes place.
  • the reaction product formed may be separated from the flue gas in a known manner by filters, including electro-filters, or separation cyclones, in particular by means of bag filters of the type described in US patent specification No. 4,197,278.
  • These bag filters may consist of woven cloth or steel web and their size and number may be dimensioned according to the demands for filtration.
  • the bag filters may be emptied at intervals determined by the desire of the principally longest residence time in the filters against an undesired growing pressure drop with increasing quantities of deposited solid material.
  • the pressure drop above the bag filters may in a known manner be counterbalanced by installing one or more suction draft blowers in the flue gas channel after the bag filters.
  • the solid product filtered off may be directed to a depot or to further processing, but it is preferred that part of the product be re ⁇ circulated for mixing with the dewpoint adjusted flue gas before addi- tion of a fresh alkaline absorption agent.
  • the inserted separator is a cyclone or a cyclone battery, whereby the residence time is prolonged.
  • a cyclone as a socalled ulti-cyclone fil ⁇ ter it is moreover possible to remove the fly ash selectively from the other solid particles.
  • the solid particles separated from the inserted separator may be directed to a depot or to processing, but it is pre- ferred that at least part of the product be recirculated together with the recirculated mixture from the bag filter to the flue gas channel.
  • the main quantity of the fresh alkaline absorption agent is added thereafter, i.e. in the preferred embodiment between the cyclone and the bag filter.
  • the fresh absorption agent is injected at a site where the flue gas has a relatively low con ⁇ tent of S0 2 and it becomes possible to remove this residual amount and other acid components such as HC1 and HF, if any.
  • the alkaline absorption agent may be added before the separator so that the desulphurization therein is increased.
  • the degree of purification obtainable by means of this embodiment of the process according to the invention depends substantially on the quantity of alkaline absorption agent added relative to the content of acid components and on the degree of recirculation.
  • the invention also relates to a fluid-bed furnace for performing the process described above, and the furnace according to the invention is characterized in that an inner wall portion of the furnace and/or of a flue gas channel connected thereto is surrounded by a mantle for cool ⁇ ing agent. It is thereby obtained that the coating forming products entrained by the flue gas settle on this cooled inner wall portion which may be situated in such a way that the coatings can easily be removed.
  • the wall portion is a cooling cyclone whereby the advantages described above in connection with the corresponding process aspect is obtained.
  • Figure 1 shows schematically a combustion plant for combustion and purifiation of flue gas waste in accordance with the process of the in ⁇ vention
  • Figure 2 shows in more detail a water cooled stack or a drop chamber forming part of the flue gas channel and which in a modified embodiment is situated immediately after the furnace, and
  • Figure 3 shows schematically a combustion plant for combustion of waste and purification of flue gas in accordance with the most preferred embodiment of the process of the invention.
  • the plant shown in Figure 1 for combustion of waste comprises a fluid-bed furnace 10, at the bottom having air distributing openings 11 in connection with a fluidization blower 12.
  • Fuel in the form of more or less comminuted waste, e.g. shredder waste, is kept in a fuel silo 13 and led from the bottom thereof to the inlet end of a screw feeder 14 by means of a conveyor band 15.
  • the screw feeder 14 leads to the furnace 10 somewhat above the air distributing openings 11, and above the inlet of the screw feeder 14 is the inlet of a silo 16 for a fluidization material, e.g. sand or lime.
  • the furnace 10 has at its lower bottom a reception chamber 17 for solid combustion products, non-inflammable materials contained in the fuel, and fluidization material.
  • mate ⁇ rials may from the chamber 17 via a valve 18 be directed downwards to a vibrating screen 19 whereby the fluidization material may be separated from the coarser substances and returned to the silo 16 as indicated with a dotted line 20.
  • the separated coarser substances may be collected in a waste container 21.
  • the flue gas generated by the combustion in the furnace 10 is led through a drop chamber 22 which at the bottom has an outlet provided with a valve 23.
  • the fuel gas may as shown be led through a convection heat surface 24 having an outlet 25 provided with a valve, and through a bag filter 26 which is also provided with an outlet 27 comprising a valve.
  • a bag filter 26 which is also provided with an outlet 27 comprising a valve.
  • the cleaned fuel gas is blown to a chimney (not shown) by means of a flue suction device 28.
  • Figure 2 shows in more detail the drop chamber 22 connected with the furnace 10.
  • the upper portion of this drop chamber having a mainly circular-cylindrical shape, is surrounded by a water mantle 29 to which e.g.
  • the drop chamber 22 is at the top provided with a cover 32 which may be opened and through which an automatically operating brushing or scraping device (not shown) may be introduced, when the cover has been opened, for removal of coatings on the inner walls of the drop chamber.
  • the drop chamber is provided with a reception chamber 33 for coating material removed by means of the cleaning device, and the loosened coating material may be removed through a gate 34.
  • the entire drop chamber 22 is appropriately enclosed by a layer of insulating mate ⁇ rial 35, e.g. mineral wool.
  • another flue gas cooler 36 which may have the shape of the convection surface 24 shown in Figure 1 or any other shape.
  • waste e.g. shredder waste
  • the conveyor band 15 and screw feeder 14 e.g. a conveyor band 15 and screw feeder 14.
  • fluidization material in the form of lime or sand are supplied as required from the silo 16.
  • fluidization blower 12 fluidization air is blown through the air distibuting openings 11 so that the fuel and the fluidization material form a fluid-bed 37, wherein a cool ng conduit 38 may be installed for obtaining the desired temperature of the fluid-bed.
  • Uncombusted material, ash and excess flui ⁇ dization material are collected gradually in the chamber 17 from where it may be directed through the valve 18 to the vibrating screen 19 where the fluidization material may be separated and returned to the silo 16 as previously described.
  • the flue gas passes through the drop chamber 22, the convection heat surface 24, the filter 26 an the flue suction device 28 to a chim ⁇ ney.
  • metal oxides and other substances in a more or less gaseous state entrained with the flue gas may settle on the inner cylindrical wall in the form of coatings.
  • the coatings formed in the chamber 22 may be removed at appropriate interval and the scraped coatings may be removed through the valve 23 in Figure 1 and through the gate 34 in Figure 2.
  • the temperature of the fluid-bed 37 may appropriately be 750- 1000°C, whereas the temperature of the flue gas when leaving the furnace 10 may appropriately be 750-1100 °C.
  • the flue gas leaves the drop chamber 22 it may be cooled down to 600-900°C. and after pas ⁇ sing the convection heat surface 24 the temperature may have fallen to 150-200°C.
  • the fluid-bed furnace 10 is of principally the same structure as the one shown at 10 in Figure 1, and analogous portions have the same reference numerals as in Figure 1.
  • fluidization air is blown in by means of the blower 12
  • waste material is introduced by means of the screw feeder 14 and solid combus ⁇ tion products
  • non-inflammable waste products and fluidization material are removed via the valve 18.
  • the flue gas generated at the combustion in the furnace 10 is directed to a cyclone 30 which analogously with the drop chamber 22 in Figure 2 may be enclosed by a water mantle having inlet and outlet of district heating water or another cooling agent.
  • the flue gas When the flue gas meets with the cooled walls of the cyclone, metal oxides and other substances entrained by the the flue gas may settle on the cyclone wall from where they are worn off by the fluidization particles entrained, preferably sand.
  • the solid material deposited in the cyclone may then be removed through the valve 23 and directed to slag depot or recirculated to the furnace in order to obtain a better burning-out of e.g. fly ash.
  • the flue gas is directed via a flue gas chan ⁇ nel 32 to a flue cooler or heat exchanger 40.
  • This may be in heat exchanging connection with an air preheater for preheating primary air for introduction into the combustion furnace 10 or it may be formed with a convection heat surface and subsequent heat spiral in order to exchange heat with a medium, such as district heating water, in a con ⁇ ventional manner.
  • a medium such as district heating water
  • From the bottom of the flue cooler 40 solids may be removed via valve 42 and directed to depot via conduit 44.
  • From the flue cooler 40 the flue gas channel leads to a separator 50 formed as a cyclone battery and from there to a battery of bag filters 60 formed as a separator. Finally, the flue gas channel leads via a suction draft blower 70 to a chimney.
  • a silo 80 is intended for storing alkaline ab ⁇ sorption agent, e.g.
  • lime hydrate which by means of a blower (not shown), e.g. a high pressure blower, is injected via a conduit 82 directly into the flue gas channel 32 at a primary insert point between the cyclone 50 and the filter 60.
  • a blower e.g. a high pressure blower
  • part of the absorption agent may be directed via a branch 84 at a secondary insert point ending in the flue gas channel 32 before the flue cooler 40.
  • the solids separated on the filter 60 are directed at the bottom by means of a valve/conveying mechanisms 62 via a conduit 66 to a receiver 68.
  • a blower (not shown) from the receiver 68 may recirculate material via conduit 69 to an intermediary insert point on the flue gas channel 32 between the flue gas cooler 40 and the cyclone battery 50. From the cyclone battery 50 separated solids are directed via valves 52 and conduit 54 to the receiver 68 from where the collected material via conduit 65 may be directed to depot or further processing or recircu ⁇ lated via conduit 69.
  • shredder waste is stoked into the furnace 10 and the volatile metal oxides, e.g. MgO and A1 2 0 3 , are separated in the cyclone 30 as explained above.
  • a small quantity of powdered lime hydrate, Ca(0H) 2 is injected via the conduit 84, whereas the remainder of the desired quantity of lime is injected in dry form via the conduit 82.
  • the flue gas has a temperature of approx. 500°C. whereby the lime neu ⁇ tralizes the content of SO.,, HC1, HF and the l ke acid products of the flue gas.
  • the flue gas is cooled to a temperature ⁇ of about 55-60°C, causing that the flue gas now has a temperature between 15-20°C. above the waterdew point subject to a usual water content in the combustion process.
  • the lime addded via the conduit 82 reacts with S0 2 , and HC1 and HF, if any, in the flue gas in accordance with the reactions.
  • Unreacted Ca(0H) 2 and the CaS0 3 , CaCl 2 and CaF 2 formed are deposited on the bag filters 60 from where the mixture is removed at suitable intervals and led to the receiver 68. From here a large quantity (approx. 10 times the quantity of weight of fresh lime) is re- circulated and the unused recirculated Ca(OH) 2 reacts with S0 2 , and HC1 and HF, if any, in the dewpoint adjusted flue gas directed to the cyclone 50 where CaS0 3 , CaCl 2 and CaF 2 are precipitated together with unreacted Ca(0H) 2 . Also this product is directed to the receiver 68 from where it is recirculated via conduit 69 or ' directed to depot via conduit 65. Fly ash not separated in the cooling cyclone 30 is separated in the cyclone 50, if desired as an individual fraction.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

Dans un procédé servant à la purification de gaz de fumée provenant de la combustion de déchets, y compris de déchets de délisseuse, dans un four se trouvant dans des conditions de lit fluidisé, et plus particulièrement dans des conditions de lit fluidisé à barbotage, les gaz de fumée chauds produits par la combustion dans le four ou dans un canal de gaz de fumée relié audit four sont mis en contact avec une surface interne refroidie, de sorte que des couches se déposent sur ladite surface et peuvent ensuite être éliminées. Dans un aspect particulier de la présente invention, les gaz de fumée sont ensuite réglés de sorte que leur température effective soit légèrement supérieure au point de rosée de l'eau, et un agent d'absorption alkalin frais est ajouté sous forme sèche. Une purification efficace des gaz de fumée, notamment en ce qui concerne le soufre, les halogénures d'hydrogène et les oxydes de métal, est ainsi obtenue.
PCT/DK1987/000141 1986-11-17 1987-11-16 Procede de purification de gaz de fumee Ceased WO1988004013A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DK5487/86 1986-11-17
DK548786A DK548786A (da) 1985-11-28 1986-11-17 Fremgangsmaade til rensning, navnlig afsvovling, af roeggas
DK6254/86 1986-12-22
DK625486A DK163802C (da) 1986-11-17 1986-12-22 Fremgangsmaade til toer-rensning af roeggas fra forbraending af affaldsmateriale, der er i hovedsagen ikke-metallisk shredderaffald

Publications (1)

Publication Number Publication Date
WO1988004013A1 true WO1988004013A1 (fr) 1988-06-02

Family

ID=26067861

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/DK1987/000141 Ceased WO1988004013A1 (fr) 1986-11-17 1987-11-16 Procede de purification de gaz de fumee

Country Status (3)

Country Link
AU (1) AU8278787A (fr)
DK (1) DK163802C (fr)
WO (1) WO1988004013A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0521844A1 (fr) * 1991-06-28 1993-01-07 Voest-Alpine Industrieanlagenbau Gmbh Procédé pour l'utilisation énergétique de déchets de ferraille déchiquetée
EP0913503A1 (fr) * 1997-10-24 1999-05-06 Leybold Systems GmbH Appareillage pour l'élimination de la poussière dans un courant de gaz
EP1547667A1 (fr) * 2003-12-23 2005-06-29 Ansaldo Ricerche S.p.A. Méthode pour la séparation de particules de fumées, en particulier de fours de fusion l'industrie de production du verre, et four de fusion correspondant
EP2397213A1 (fr) 2010-06-18 2011-12-21 Lab Sa Procédé de gestion du risque de corrosion dans des procédés de traitement de fumées

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3257777A (en) * 1961-01-31 1966-06-28 Demag Elektrometallurgie Gmbh Process for treating waste gases
EP0033356A1 (fr) * 1980-01-30 1981-08-12 Deutsche Babcock Aktiengesellschaft Dispositif pour la combustion de matières avec des composants difficiles à brûler
FI60134B (fi) * 1977-06-02 1981-08-31 Ahlstroem Oy Foerfarande och anordning foer rening av gaser innehaollande smaelta och foeraongade komponenter
US4340400A (en) * 1980-09-10 1982-07-20 Centro Ricerche Fiat S.P.A. Fluidized bed filtering and/or heat exchange apparatus particularly for gaseous discharges from internal combustion engines and industrial plants
DE3345330A1 (de) * 1983-12-15 1985-07-04 L. & C. Steinmüller GmbH, 5270 Gummersbach Verfahren zur bindung von schwefelverbindungen, die als reaktionsprodukte bei der verbrennung schwefelhaltiger brennstoffe in einer schuettbett- oder fliessbettfeuerung ...

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3257777A (en) * 1961-01-31 1966-06-28 Demag Elektrometallurgie Gmbh Process for treating waste gases
FI60134B (fi) * 1977-06-02 1981-08-31 Ahlstroem Oy Foerfarande och anordning foer rening av gaser innehaollande smaelta och foeraongade komponenter
EP0033356A1 (fr) * 1980-01-30 1981-08-12 Deutsche Babcock Aktiengesellschaft Dispositif pour la combustion de matières avec des composants difficiles à brûler
US4340400A (en) * 1980-09-10 1982-07-20 Centro Ricerche Fiat S.P.A. Fluidized bed filtering and/or heat exchange apparatus particularly for gaseous discharges from internal combustion engines and industrial plants
DE3345330A1 (de) * 1983-12-15 1985-07-04 L. & C. Steinmüller GmbH, 5270 Gummersbach Verfahren zur bindung von schwefelverbindungen, die als reaktionsprodukte bei der verbrennung schwefelhaltiger brennstoffe in einer schuettbett- oder fliessbettfeuerung ...

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0521844A1 (fr) * 1991-06-28 1993-01-07 Voest-Alpine Industrieanlagenbau Gmbh Procédé pour l'utilisation énergétique de déchets de ferraille déchiquetée
EP0913503A1 (fr) * 1997-10-24 1999-05-06 Leybold Systems GmbH Appareillage pour l'élimination de la poussière dans un courant de gaz
EP1547667A1 (fr) * 2003-12-23 2005-06-29 Ansaldo Ricerche S.p.A. Méthode pour la séparation de particules de fumées, en particulier de fours de fusion l'industrie de production du verre, et four de fusion correspondant
EP2397213A1 (fr) 2010-06-18 2011-12-21 Lab Sa Procédé de gestion du risque de corrosion dans des procédés de traitement de fumées
FR2961408A1 (fr) * 2010-06-18 2011-12-23 Lab Sa Procede de gestion du risque de corrosion dans des procedes de traitement de fumees

Also Published As

Publication number Publication date
DK625486A (da) 1988-05-18
DK163802B (da) 1992-04-06
DK163802C (da) 1992-09-07
AU8278787A (en) 1988-06-16
DK625486D0 (da) 1986-12-22

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