EP0754247A1 - Procede et systeme de traitement thermique de materiaux - Google Patents

Procede et systeme de traitement thermique de materiaux

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Publication number
EP0754247A1
EP0754247A1 EP95913086A EP95913086A EP0754247A1 EP 0754247 A1 EP0754247 A1 EP 0754247A1 EP 95913086 A EP95913086 A EP 95913086A EP 95913086 A EP95913086 A EP 95913086A EP 0754247 A1 EP0754247 A1 EP 0754247A1
Authority
EP
European Patent Office
Prior art keywords
treatment
treatment bed
bed
treated
ignition
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
EP95913086A
Other languages
German (de)
English (en)
Other versions
EP0754247B1 (fr
Inventor
Hermann BRÜGGENDICK
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.)
Steag Energy Services GmbH
Original Assignee
Steag GmbH
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 DE4411505A external-priority patent/DE4411505C1/de
Priority claimed from DE4431939A external-priority patent/DE4431939C1/de
Application filed by Steag GmbH filed Critical Steag GmbH
Publication of EP0754247A1 publication Critical patent/EP0754247A1/fr
Application granted granted Critical
Publication of EP0754247B1 publication Critical patent/EP0754247B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B21/00—Open or uncovered sintering apparatus; Other heat-treatment apparatus of like construction
    • F27B21/06—Endless-strand sintering machines
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/16—Sintering; Agglomerating
    • C22B1/20—Sintering; Agglomerating in sintering machines with movable grates

Definitions

  • the invention relates to a method for the heat treatment of a pourable material to be treated, in particular for sintering metallic materials according to the preamble of patent claim 1. Furthermore, the invention relates to an arrangement according to the preamble of patent claim 13.
  • FIG. A in which a conventional sintering system with the first additional units is shown schematically as a treatment system.
  • FIG. A essentially consists of a sintering plant 1 with an ignition furnace 3 arranged at its inlet end, a sintering bed transport device 5 which has an endless sintering belt 7 guided through the sintering plant, a sintering mixture Feed device 9 and an exhaust gas extraction device 11, with the aid of which the pressure gradient for the sintering process, which runs from top to bottom through the sintering bed, is also built up.
  • the sintering mixture in the known sintering process described with reference to FIG. A consists of ores, additives, fuels, in particular coke breeze, quicklime and return material from the sintering process itself.
  • a mixing and rolling drum 13 ensures an intimate mixture of the granular or pourable mixture components as well as a uniform grain size and shape of the sintered material.
  • the feed device 9 is fed from the mixing and rolling drum 13 and pours the sinter mixture in a substantially uniform layer thickness onto the grate of the sintering belt 7.
  • a finished sintered layer is applied to the grate in this known system Sintered belt 7, which is arranged between the actual sintering bed, ie the sintering mixture layer and the grate and protects the grate from excessive temperature loads and stresses in the manner of a temperature barrier.
  • the finished sintered layer remains in the This is unaffected by the subsequent sintering process in the sintering plant 1 and does not interfere with the postprocessing steps in a breaker 17, in a sinter cooler 19 and in a cold sieve station 21 until the usable finished sinter is obtained at the starting point 23.
  • the associated conventional sintering process takes place as follows: First, a suitable rust coating layer is applied uniformly to the sintering belt 7 via the feed device 15. The sintered mixture is poured onto the grate covering in a predetermined layer thickness over the full width of the bed as evenly as possible. The sintering belt 7 moves from the feeding point of the sintering mixture below the feeding device 9 to the left towards the sintering plant. The sintering bed is ignited by the ignition furnace 3 on the first side facing it when it enters the sintering plant 1.
  • a pressure drop is built up in the entire sintering system 1 in the sintering bed through the extraction device 11 below the bed, through which combustion air is introduced into the combustible sintering mixture and exhaust gases are removed on the second sintering bed side (underside).
  • a combustion zone forms in the sintering bed, which moves from top to bottom in the sintering bed from right to left as the sintering bed progresses, the sintered material being sintered through in this zone and come to cake
  • the course and the formation of the firing or sintering zone over the depth of the sintering bed can be seen from the length of the sintering belt in the interior of the sintering plant 1 from FIG.
  • the bed depth is 500 mm.
  • the firing or sintering zone reaches the bottom of the sintering bed at the end of the sintering process or shortly before it emerges from the sintering plant 1 and softens the material to be sintered there so far that the individual material Baking grains together (agglomerating).
  • the invention is therefore based on the object of removing the pollutants produced in heat treatment processes of the generic type as far as possible and with comparatively little investment, preferably with a reduction in the volume of exhaust gas to be cleaned.
  • the invention is based on the knowledge that the conventional sintering process described already inherently contains numerous properties and phases which favor exhaust gas cleaning, which could not previously be suitably used. This is only possible according to the invention, namely in terms of the method with the features of claims 1, 2, 3, 4 and 6 and in terms of arrangement with the features of claims 13, 14, 15 and 16.
  • the invention is based on the secondary-side exhaust gas purification measures for very large gas volumes which are burdened with extremely high investment costs. In all alternative solutions, it essentially integrates exhaust gas purification into the primary sintering process.
  • the invention is based on the consideration that, in the known type of heat treatment, a strongly adsorbing filter layer is connected downstream of the combustion zone as long as the combustion zone has not yet broken through to the flue gas side opposite the ignition side.
  • the Reini- The effect of this "natural" adsorption view is used in the invention. Before the cleaning effect disappears due to the combustion of the carbon-containing (adsorbable) fuel and the combustion zone penetrates to the other side, the pressure drop is reversed in the first solution according to the invention and counter-combustion is generated.
  • the second burning zone migrating into the bed from the other side is in turn followed by a layer which can initially act as a filter layer.
  • organic chlorine substances released for example dioxins or furans, are burned in the second firing zone under the influence of the high temperature of the first firing zone or adsorbed by remaining carbon particles and subsequently burned in the same way.
  • the exhaust gases emerging from the treatment bed are collected and passed into the ignition furnace.
  • either all of the gases emerging in the treatment system can be recycled or only the gases from partial phases which have a critical pollutant content, in particular the end phase of the treatment process.
  • the pollutants contained in the exhaust gases are destroyed by the influence of the high temperature in the ignition furnace.
  • the exhaust gases are then passed through the treatment bed under the influence of the pressure gradient applied to the treatment bed. They are exposed to extremely high temperatures in the area of the firing zone and are further cleaned in this way.
  • the "natural" cleaning layer formed in the treatment bed behind the firing zone also adsorbs residual pollutants remaining in the exhaust gas.
  • the exhaust gases emerging from the treatment bed in the final phase of the process are collected and passed through the treatment bed together with the gases required for heat treatment in the initial and / or middle phase of the process.
  • the exhaust gases can be distributed over a large area over the treatment bed and passed through it.
  • the pollutants So they are not concentrated in the area of the ignition furnace, but can be supplied together with combustion air in a lower concentration.
  • the pollutants contained in the exhaust gases for example dioxins and furans, are in turn destroyed under the influence of the high temperature when the gas mixture passes through the combustion zone.
  • the cleaning action of the "natural" adsorption layer formed behind the firing zone is also used in this method alternative. Only minor technical conversion measures are required to implement the method, so that the costs incurred are comparatively low.
  • the pressure drop and thus the burning of the fuel layers within the bed is maintained from the beginning to the end of the treatment process. While the burning zone is moving from top to bottom, the relatively cool, untreated mixture layer underneath acts as an adsorption filter. Their filter effect is enhanced by the lowest (first) layer made of adsorptive material, especially coke. This layer is protected from ignition by the second layer of inert material acting as a temperature barrier. It is therefore an adsorption filter layer carried in the primary process. Instead of lumpy or granular coal or coke, other lumpy or granular materials can be used which have comparable adsorption or filter properties.
  • the last-mentioned alternative method makes a change to the conventional treatment system superfluous.
  • the adsorbent-forming coke is poured onto the grate supporting the layer sequence as the first layer and accompanies the actual treatment process as a primary filter.
  • This layer of coke is not lost; because on the one hand the coke can be largely separated from the remaining layers at the end of the treatment process and can possibly be recycled and reused, and on the other hand it can be used as a Top layer uses coke in the blast furnace to replace other coke feed materials.
  • the pollutants are concentrated on the system section in which the exhaust gas temperature is particularly high by a targeted shift of the pollutant profile in the direction of the profile of the exhaust gas temperature and in particular by superimposing the associated profile maxima.
  • the cleaning of the exhaust gases can therefore be limited to a correspondingly short section of the treatment area in which the pollutant concentration and exhaust gas temperature are at a maximum. In this way, cleaning plants of small capacity are sufficient to operate an entire treatment plant with very low pollutant emissions.
  • the shift in the pollutant concentration profiles is achieved by enriching the treatment bed with pollutant adsorbing agents which retain the pollutants up to the last section of the treatment area (e.g. the sintering machine). Only at the end of the treatment area, when the capacity of the pollutant-adsorbing agent is exhausted and the combustion zone reaches those lower layers in which the pollutants have been retained in a highly concentrated manner, does the concentration of the pollutants in the exhaust gas increase sharply. This portion of the exhaust gases which is heavily polluted can then be cleaned separately.
  • agents with improved adsorption properties can be used in the applications in which the treatment process requires the use of pollutant-adsorbing agents in the treatment bed.
  • a larger specific surface of the individual adsorbent particles can, for example, already lead to the desired shift in the pollutant concentration profiles.
  • the pollutant-adsorbing agents are advantageously mixed with the material to be treated and then poured onto the grate before they are introduced into the treatment area. So it succeeds almost without additional technical effort, that Distribute pollutant adsorbents evenly in the treatment bed.
  • the pollutant-adsorbing agents are present in a higher concentration in the lower region of the treatment bed than in the upper region of the treatment bed.
  • Different concentration ratios between pollutant-absorbing agents and the material to be treated can be produced during mixing.
  • a preferred embodiment is characterized in that the collected exhaust gases are catalytically cleaned using their high temperature. Effective catalytic cleaning is only possible at temperatures above 300 ° C. By superimposing the pollutant concentration max a with the temperature maximum, the high temperature required for catalytic cleaning is reached in most heat treatment processes. No additional thermal energy has to be supplied; instead, the heat energy released in the heat treatment process is collected and sufficient as a heat supplier. It is also advantageous that the heat is not released into the environment as waste heat.
  • Various types of pollutants can be removed from the exhaust gas by catalytic cleaning; For example, organochlorine substances such as dioxins and furans can be reduced using suitable reduction catalysts. Nitrogen oxides can also be easily reduced at these temperatures.
  • a catalytic oxidation is possible, for example, for pollutants such as SO2. SO2 becomes SO3 through oxidation.
  • the pollutant-adsorbing agents and their concentrations in the treatment bed are selected such that the concentrations tion profiles of the pollutants arising in the treatment process and in particular their maxima are brought to overlap in the end section of the treatment area.
  • concentration profiles of different pollutants can be overlapped with one another and the steeper the concentration peaks, the smaller the partial volume of the exhaust gas to be cleaned and the more effectively the method according to the invention works.
  • the exhaust gases emerging from the treatment bed in the last phase are subjected to particle separation.
  • a normal electrostatic filter can be used for this purpose. In order to achieve a particularly high cleaning effect, it is favorable to use catalytic cleaning after the particle separation.
  • the exhaust gas can be washed with adsorbent and water after the catalytic cleaning. This is done, for example, with the aid of a spray dryer, in which dust-like carbon-containing adsorbent and water are introduced into the flue gas stream.
  • the water introduced reduces the exhaust gas temperature to such an extent that, for example, salts and chlorides can crystallize out.
  • an activated coke system can be used instead of or in addition to a spray dryer.
  • the exhaust gas is advantageously subjected to particle separation.
  • a part of the solids resulting from the particle separation can be recycled and used again as an adsorbent for cleaning. Since the adsorbent-containing solids cannot fully utilize their absorption capacity of pollutants on their first passage through the exhaust gas, the recycling makes it possible to load the adsorbent with pollutants up to its capacity limit and to keep the operating costs low.
  • Carbonaceous, pourable material for example coke breeze and / or activated coke, is advantageously used as the pollutant adsorbent. This material is inexpensive to purchase. In the case of heat treatments above the ignition temperature of coke breeze, it ignites and releases the heat of combustion released as additional heat to the treatment bed. No disturbing foreign substances remain in the treatment bed.
  • the method according to the invention is preferably used in the sintering of metallic materials.
  • 1 shows a schematic representation of a sintering arrangement for carrying out a first sintering process according to the invention
  • 2 shows a schematic representation of a sintering arrangement for carrying out a second method alternative according to the invention
  • 3 shows a schematic representation of a sintering arrangement for carrying out a third method alternative according to the invention.
  • 4 shows a schematic representation of a sintering arrangement for carrying out a fourth treatment method according to the invention
  • 5 shows a schematic representation of a sintering arrangement for carrying out a fifth method alternative according to the invention
  • 6 shows a schematic illustration of a sintering arrangement for carrying out a sixth method alternative according to the invention
  • 7a shows a schematic representation of a sintering arrangement
  • 7b shows a diagram of the exhaust gas temperature, plotted against the length of the sintering belt
  • 7c shows a diagram of the exhaust gas concentration of S02, plotted against the length of the sintering belt
  • 7d shows a diagram of the exhaust gas concentration of polychlorinated dibenzodioxins and polychlorinated dibenzofurans, plotted against the length of the sintered belt
  • 7e shows a diagram of the exhaust gas concentration of nitrogen oxides, plotted against the length of the sintered belt.
  • FIG. 1 differs from the conventional sintering arrangement in FIG. A on the one hand by a second ignition furnace 4, which is arranged near the outlet end of the sintering system 1 and ignites the sintering bed from the underside, and on ⁇ on the other hand by a device for generating a pressure drop in the opposite direction, ie from the bottom of the bed to the top of the bed.
  • This pressure gradient generating device has an exhaust gas exhaust hood 6 and a suction pump 10 arranged in a return line 8.
  • the exhaust gas discharged via the extractor hood 6 can be dedusted using a suitable filter 12.
  • a suitable filter 12 In a mixer 14, the exhaust gas is mixed with the combustion air required in the front or middle area of the sintering system 1 and is passed together with the combustion air through the hood 16 through the sintering bed from top to bottom.
  • the organochlorine substances When passing through the firing zone or through the high temperature area of the sintered bed passed through the firing zone, the organochlorine substances are destroyed with sufficient reliability.
  • the exhaust gases which are recirculated or newly formed during sintering pass through the sintered mixture, in which the highly carbon-containing fuel is generally contained in fine form in the form of coke breeze.
  • This fuel acts as an adsorbent, in which a substantial part of the pollutants is similar as in conventional secondary purification of exhaust gases in activated coke reactors.
  • the sintering belt 7 is assigned three feed devices in succession.
  • a thin adsorbent layer 20 is applied to the grate.
  • A is arranged behind the device 18, the application device 15 already described with reference to FIG. A for the application of the finished sintered layer 22 to the adsorbent layer 20, and then the application device 9 for the application of the sintering mixture 24, which represents the actual sintering bed, follows.
  • the finished sintered layer 22 which can also consist of another material with essentially inert properties, forms a temperature barrier which prevents the firing zone from spreading into the adsorptive filter layer 20.
  • FIG. 3 shows a sintering arrangement which is basically similar to that of FIG. 1, but in which the second ignition furnace 4 is missing in the rear section of the sintering arrangement 1.
  • an exhaust gas collection device 6 ' is provided there, but is arranged at the normal pressure drop on the underside of the sintered bed.
  • the exhaust gas collected there is returned to the mixing device 14 via the return line 8 and the suction pump 10, mixed there with combustion air and passed through the sintering bed via the hood 16 in the front and middle region of the sintering system 1.
  • the cleaning effect of the sinter mixture located beyond the firing zone in the sinter bed is also used in this arrangement according to FIG. 3.
  • the investment costs are primarily lower because the second ignition device is superfluous and the additional filter system 12 can also be omitted.
  • the primary emission control measures described above can also be used in combination.
  • the exhaust gas recirculation according to FIG. 3 can of course also be used when using the additional adsorbent layer 20 according to FIG. 2.
  • the exhaust gas can be fed back only into the ignition furnace and only into the inlet-side or central section of the sintering system outside the ignition furnace. In the same way, however, it can be fed back into the ignition furnace area and a further area, for example into the middle section of the sintering plant.
  • the mixer 14 and / or the hood 16 can be dispensed with.
  • the invention also does not require any restrictions with regard to the sintered bed conveying device.
  • the conventional sintering belt system can be replaced, for example, by a so-called push-through furnace, in which the sintering bed is moved in baskets arranged one behind the other and pushed through the sintering system 1.
  • the conveyor belt can be driven both continuously and discontinuously.
  • the feed device 9 serves not only to supply the sinter mixture, but also an additional adsorbent.
  • the sinter mixture consists in a known manner of ores, additives, fuels, in particular coke breeze, quicklime and return material from the sintering process itself.
  • the adsorbent contains carbon and is granular or pourable.
  • exhaust line 25 drawn off in the front and middle sections of the sintering system with the exhaust gas extraction device 11 can, after particle separation with an electrostatic filter 25 ', pass to the ambient atmosphere without further cleaning steps be dissipated.
  • the discharge drawn off by the exhaust gas extraction device 11 in the rear section of the sintering system 1 is conducted via a separate extraction line 26. In this section of the sintering plant, the temperature of the exhaust gas is naturally particularly high.
  • the maximum concentration of all critical pollutants for example any chlorine-organic substances, nitrogen oxides and sulfur dioxide, also lies in this last section.
  • Particles such as fly ash are first separated out of the exhaust gas with the electrostatic filter 27.
  • the exhaust gases are then catalytically cleaned with the addition of reducing agents.
  • any dioxins and furans and nitrogen oxides that may be present are reduced with a reduction catalyst.
  • An additional oxidation catalyst is used to oxidize SO2 to SO3.
  • the catalytic treatment is favored by the high exhaust gas temperature.
  • the catalytically cleaned exhaust gas can then be released into the ambient atmosphere without further purification (exhaust line 29).
  • the fifth embodiment of the arrangement according to the invention shown in FIG. 5 differs from the arrangement shown in FIG. 4 by the cleaning arrangement connected downstream of the exhaust gas discharge line 26.
  • the catalytic cleaning reactor 28 is acted upon directly by the pollutant-elastic exhaust gases.
  • the exhaust gases are then cleaned in an adsorbent reactor 30, with the addition of adsorbent and water, of sulfur oxides, dust and organic substances.
  • a fabric filter 31 connected downstream of the adsorbent reactor 30 separates the loaded adsorbent and other solids from the flue gas stream.
  • the filtrate is partly returned to the reactor via the return line 32 in order to adsorb further pollutants there and to fully utilize the adsorption capacity of the particles.
  • the exhaust gas After the fabric filter 31, the exhaust gas has a relatively high purity and can be discharged together with the exhaust gas from the exhaust line 25 into the ambient atmosphere.
  • the exhaust gas in this embodiment also fills the ever stricter pollutant emission limits and is particularly environmentally compatible.
  • the adsorbent reactor 30 used can be designed to be very small, since by concentrating the release of pollutants on the rear section of the sintered area, only a small part of the exhaust gas removed during the heat treatment process has to be cleaned of pollutants. The construction effort remains low. By returning the adsorbent to the reactor, the operating costs are also kept low.
  • the exhaust line 26 first leads to the electrostatic filter 27, in which solids, in particular fly ash, are separated.
  • the actual cleaning again takes place in the catalytic cleaning reactor 28 at temperatures of approximately 300-400 ° C.
  • the hot exhaust gas is then returned to the ignition furnace via a return line 33.
  • the exhaust gas is mixed with combustion air and passed through the sintered bed again.
  • the cleaning effect of the sintering mixture located beyond the firing zone in the sintering bed is used in order to achieve an even higher purity of the exhaust gas.
  • the exhaust gas purification measures described can also be used in combination.
  • the exhaust gas recirculation according to FIG. 6 can of course also be used in addition to an adsorbent reactor.
  • the adsorbent can be introduced in the lower layers of the sintered bed in a higher concentration than in the upper layers.
  • the adsorbent and the sintered mixture can also be applied to the belt one after the other.
  • a separate adsorbent layer can be provided separated from the sintered mixture by an insulation layer.
  • Such an adsorbent layer can also be used in addition to enriching the material to be treated with adsorbable material.
  • the adsorbent itself can be an additive and / or one used in conventional sintering processes Be a mixture of substances whose pollutant-adsorbing properties are improved in the sense of the invention. It is important that the concentration profile of the pollutants is shifted to match the exhaust gas temperature profile. This is explained in more detail below with reference to FIG. 7.
  • the sintering process begins below the ignition furnace 3.
  • the sintering belt 7 moves in the conveying direction, that is to the right in the drawing. Simultaneously with the conveying movement of the sinter bed, the sinter zone moves from top to bottom through the sinter bed.
  • FIG. 7a shows a diagram of the exhaust gas temperatures, plotted against the sintering belt length.
  • the solid line represents the curve for a conventional sintering process and the dashed line represents the curve for the method according to the invention.
  • the course of the exhaust gas temperature shows a strong maximum in the rear section of the sintering region, both in the known method and in the method according to the invention.
  • the temperature profile is practically not affected by the invention.
  • FIG. 7b shows the diagram of the concentrations of SO2 in the exhaust gas, plotted against the sintering band length.
  • solid line the SO2 concentration in the exhaust gas rises shortly behind the center of the sintering system.
  • the S ⁇ 2 ⁇ peak is very broad.
  • the exhaust gas concentration of the SO2 is constantly significantly lower in the front and middle sections and only increases significantly later with a relatively steep flank. The peak is shifted backwards and considerably narrower.
  • FIG. 7c shows the exhaust gas concentrations of polychlorinated dibenzodioxins and dibenzofurans against the sintering band length.
  • concentration of organochlorine substances increases in the middle of the sintering process. Analogous to the peak of the SO2 exhaust gas concentration, the peak is very broad.
  • the exhaust gas loading with organochlorine substances in the front and middle sections is achieved by the additional The adsorption effect of the sintered bed was significantly reduced and the maximum shifted backwards with the formation of a sharper peak.
  • the exhaust gas concentrations of NO x are plotted against the sintering belt length in FIG. 7e.
  • the NO x concentration is constant over almost the entire length of the sintering belt. Only at the end of the band does the NO x concentration drop approximately linearly. The consequence of this is that up to now the entire exhaust gas volume had to be cleaned in order to remove the NO x pollutants.
  • the exhaust gas concentration of NO x in the process according to the invention is negligibly low in the front and middle sections and only rises to a peak in the rear section of the sintering belt.
  • the method according to the invention thus enables the pollutants to be concentrated in the rear section of the sintering belt.
  • the pollutant peaks are shifted backwards and the concentration maxima correspond to the maximum of the exhaust gas temperature. In this way, only a small part of the resulting exhaust gas volume needs to be cleaned.
  • the partial exhaust gas quantity to be cleaned is collected in the rear section of the sintering machine, that is to say where the exhaust gas temperature has essentially reached the optimum temperature for catalytic cleaning.
  • FIGS. 1-6 can be combined with one another as desired.
  • the process can be used for many heat treatment processes with similar advantages, in particular also for roasting processes, for example for the heat treatment of metal sulfides, in particular lead, zinc and nickel in an oxidizing atmosphere.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Materials Engineering (AREA)
  • Environmental & Geological Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Treating Waste Gases (AREA)

Abstract

Le système comprend une bande transporteuse (7) sur laquelle un dispositif (9) dépose un mélange de frittage en vrac. La bande transporteuse achemine ce mélange à travers une installation d'agglomération par frittage (1) dans la zone d'entrée de laquelle est monté un four d'allumage (3) qui allume la face supérieure du lit de frittage. Un dispositif d'extraction (11) aménagé sous le lit de frittage aspire la zone d'incandescence vers le bas dans le lit de frittage. Dans la zone de sortie de l'installation d'agglomération par frittage (1), en dessous du lit de frittage, il est prévu un second four d'allumage (4) qui allume la face inférieure du lit de frittage. Un second dispositif d'extraction (6) aspire la seconde zone d'incandescence vers le haut. La teneur en substances nocives des gaz brûlés est considérablement réduite, du fait que dans la zone située côté entrée, les constituants non agglomérés par frittage font office de filtre, tandis que, dans la zone située côté sortie, la postcombustion des substances nocives s'effectue dans la zone d'incandescence supérieure. Un adsorbant additionnel permet en outre aux substances nocives de sortir essentiellement dans la zone de sortie de l'installation d'agglomération par frittage.
EP95913086A 1994-04-06 1995-03-11 Procede et systeme de traitement thermique de materiaux Expired - Lifetime EP0754247B1 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE4411505A DE4411505C1 (de) 1994-03-31 1994-04-06 Verfahren und Anordnung zum Sintern metalloxidhaltiger Werkstoffe
DE4411505 1994-04-06
DE4431939 1994-09-08
DE4431939A DE4431939C1 (de) 1994-09-08 1994-09-08 Verfahren und Anordnung zur Wärmebehandlung von schüttfähigem Behandlungsgut
PCT/EP1995/000906 WO1995027802A1 (fr) 1994-04-06 1995-03-11 Procede et systeme de traitement thermique de materiaux

Publications (2)

Publication Number Publication Date
EP0754247A1 true EP0754247A1 (fr) 1997-01-22
EP0754247B1 EP0754247B1 (fr) 2000-08-09

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EP95913086A Expired - Lifetime EP0754247B1 (fr) 1994-04-06 1995-03-11 Procede et systeme de traitement thermique de materiaux

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EP (1) EP0754247B1 (fr)
CA (1) CA2184843A1 (fr)
WO (1) WO1995027802A1 (fr)

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GB2347940A (en) * 1999-03-19 2000-09-20 British Steel Plc Iron ore sintering process with reduced emissions of toxic gases
DE102012005180A1 (de) 2012-03-16 2013-09-19 Gkn Sinter Metals Holding Gmbh Sinterofen mit einer Gasabführvorrichtung

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EP0754247B1 (fr) 2000-08-09
WO1995027802A1 (fr) 1995-10-19

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