EP1164331B1 - Recirculation des gaz de combustion d'un incinérateur d'ordures - Google Patents

Recirculation des gaz de combustion d'un incinérateur d'ordures Download PDF

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Publication number
EP1164331B1
EP1164331B1 EP01202285A EP01202285A EP1164331B1 EP 1164331 B1 EP1164331 B1 EP 1164331B1 EP 01202285 A EP01202285 A EP 01202285A EP 01202285 A EP01202285 A EP 01202285A EP 1164331 B1 EP1164331 B1 EP 1164331B1
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Prior art keywords
gas
waste
incineration
zone
primary
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German (de)
English (en)
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EP1164331A1 (fr
Inventor
Marcellus Antonius Jozef Van Berlo
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Gemeente Amsterdam Gemeentelijke Dienst Afvalverwerking
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Gemeente Amsterdam Gemeentelijke Dienst Afvalverwerking
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    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00Combustion
    • F23G2202/10Combustion in two or more stages
    • F23G2202/101Combustion in two or more stages with controlled oxidant supply
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00Combustion
    • F23G2202/10Combustion in two or more stages
    • F23G2202/106Combustion in two or more stages with recirculation of unburned solid or gaseous matter into combustion chamber
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00Waste heat recuperation
    • F23G2206/10Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying

Definitions

  • the invention in question relates to a method for burning waste in a waste incinerator according to the preamble of claim 1, as well as a high efficiency waste incinerator.
  • Waste incinerators and the way in which they work, are known in practice.
  • the waste material to be incinerated is placed on a support with holes in it, generally known as the incinerator grid, wherein combustion air as primary gas is brought from below up through the incinerator grid and the waste material.
  • This combustion air supplies the necessary oxygen required for the incineration.
  • This air is often pre-heated in order to make the waste burn better, since the hot combustion air has a heating effect on the material to be incinerated, and also partly helps to dry the waste material so that it is easier to ignite.
  • the invention aims at providing an improved technique as mentioned in the opening words, wherein these drawbacks can be lessened.
  • the invention aims at providing a technique wherein the efficiency of the installation can be improved and wherein the emission of dangerous substances can be lessened.
  • the invention provides a method as described in the preamble, which is characterised by the features of the characterizing part of claim 1.
  • a method according to the invention can especially be advantageously carried out using the measures as described in the claims stated later in this document.
  • a primary gas is used in the first zone that has a low oxygen content. Because of the low oxygen content, an increase in temperature does not automatically result in the waste material actually combusting. Therefore, even a temperature higher than 300°C, for example 450°C or higher, can also be applied. Because the primary gas serves in the first instance to heat and dry the compact parts of the waste material, in principle this does not result in any problems. In the second instance the easily combustible parts of the waste material combust as a result of the primary part gas supply, which therefore takes place with a deficiency of oxygen. This means that the incineration on the waste bed only partly takes place.
  • the primary gas in the first zone serves in the first place to dry the waste material that has been placed in the incinerator.
  • the primary gas that is supplied to the first zone is fed in at a temperature from 50°C to 300°C, preferably from 150°C to 300°C.
  • the pre-heating of the primary gas for a waste incinerator requires a great deal of energy, and is especially necessary if the waste material is difficult to burn. The pre-heating of the primary gases is therefore dependent on the so-called thermal value of the waste material.
  • the primary gas is at a temperature of approximately 100°C in the case of a thermal value of 11,000 kilojoules per kilogram, while the temperature of the primary gases should be approximately 180°C in the case of waste material with a thermal value of around 7,000 kilojoules. These values are based on the use of air as the primary gas, both as pre-heating and as ignition gas.
  • the waste material that is placed in a waste incinerator for incineration varies enormously both in its content and its humidity.
  • the dampness that can exist in the waste material it is important how this dampness is spread through the waste material. If one part of the waste material is relatively dry and therefore easily combustible, this part will ensure that the damper waste material surrounding it will dry rapidly and thereby combust. In practice the dry and damp parts of the waste material are not homogeneously divided, so the combustion takes place in a very irregular way.
  • Waste material that is easily combustible and has a high thermal value demands a very low pre-heating of the primary gas. If air pre-heating is used, this results in a very fierce fire above the waste bed, wherein the firing in the waste bed is very strongly sub-stoichiometric, which results in very high temperatures locally in the incineration chamber. In this case air pre-heating is unnecessary.
  • Waste material that is easily combustible but that has a low thermal value also does not require air pre-heating. In addition, there is less chance of a strong sub-stoichiometric combustion.
  • Waste material that is not easily combustible and that has a high thermal value requires primary air at a high temperature in order to achieve enough combustion of the waste material on the one hand, and on the other hand because of this the actual burning of the waste material will easily result in a simple sub-stoichiometric combustion. A careful regulation of the temperature of the primary gases is therefore necessary to control the combustion.
  • the invention provides an improved technique as stated previously, wherein the temperature is controlled for each partial primary gas supply.
  • This enables a regulation wherein the temperature of the primary gas is increased only in the zones where it is necessary, because of the composition of the waste material.
  • the primary gas that is supplied to the first zone is at a temperature of from 50°C to 450°C, preferably in the range 50°C to 300°C, with the strongest preference for the range 150°C to 300°C.
  • the aim is to choose a temperature in the first zone that is so high that in many cases pre-heating can be reduced to zero in the other zones.
  • a relatively low airflow for the first zone from 5% to 15% of the total primary airflow
  • relatively little energy is used for the pre-heating.
  • the figure shows a schematic outline of a waste incinerator according to the preferred design of the invention.
  • the incinerator shown has four different part gas supplies for primary gas (1, 2, 3, 4). These are introduced under the incinerator grid (5), on top of which is the waste bed (6).
  • the supply pipes for the first, second and third part supplies of the primary gas are equipped with an air pre-heater (7, 8).
  • Waste material is placed on the incinerator grid (5) above the first primary gas supply (1), wherein it is pervaded from below by waste gas that originates from the waste incinerator.
  • This waste gas has a low oxygen content.
  • the primary gas from the first part gas supply (1) will flow through the waste bed (6) by means of the available gas channels.
  • the waste material that comes into direct contact with such a channel is dried more than the rest of the waste material. If the partly dried waste material is moved on to a position where the second part of the primary gas (2) is supplied, because this secondary part of the supply contains oxygen, the flame front is practically immediately progressing downwards through these channels.
  • the flue gases that are formed in the flame front above the waste bed are not made up of homogeneous parts. Because of the inhomogeneous composition of the waste material, some parts of it are well incinerated and therefore in those places the oxygen in the primary gas will have reacted. In other parts, where the incineration has not taken place to any large extent, part of the oxygen supplied by the primary gas supply will not have reacted and thereby will remain in the flue gas. By adding a secondary gas a good mix of these flue gasses can be achieved.
  • an oxygen bearing gas is supplied with an adequate O 2 content (preferably a surplus) in order to burn off the remaining CO and any other possible combustible waste products in the flue gases. Because this occurs downstream, the flue gases are homogenous and already somewhat cooler and so the formation of nitrous oxides is less. Especially the fact that the flue gases are now already mixed, local peak temperatures that cause the most formation of nitrous oxides do not arise.
  • the subdivision of the supply of primary gas into several zones, as shown in the four zones in the illustration (1, 2, 3, 4), which successively pass through the waste material to be incinerated (6) achieves an optimum combustion. This can especially be achieved because the temperature can be independently regulated for each zone. Because in practice it is difficult to judge the thermal value of the waste material and its ignition behaviour in advance well enough to depend on it, the regulation of the temperature setting of the primary gas takes place by tracking the flame front for each zone. This can be done by hand or via an automatic measurement of the flame front with the help of video cameras for visible light and/or infrared light.
  • the primary gases that are supplied to the first zone (1) can be of a high temperature without any problem, because the oxygen content of these is very low.
  • the oxygen content can be 0% by volume or more.
  • the incineration above the first zone is therefore limited.
  • the maximum temperature of the flames in the first zone is thereby reduced in proportion to the available oxygen percentage, wherein no damage to the waste grid can arise. In particular damage by drops of melted metal that weld themselves to the surface of the grid is avoided. With current techniques wherein a water-cooled grid is usually used, it is not possible to obtain this advantage to such a high degree.
  • the reaction of waste gas in the first zone is also limited.
  • the waste material can therefore be fully pre-dried without all the material being incinerated in the first zone. This results in a good combustion situation in the second zone, where it is possible that no more air pre-heating is necessary, but where the incineration can still be well regulated.
  • a homogeneous incineration can especially be achieved in the second zone when the incinerator grid (5) is placed at a lower point, as described earlier.
  • the waste gas recirculation is supplied as the primary gas in the first zone.
  • the waste gas from the incinerator flue after passing through a dust filter (11) are recirculated to the first zone.
  • the oxygen percentage and the temperature are in this case reasonably firmly fixed (depending on the process design) and cannot be used for the actual control of the combustion process.
  • the amount (the flow) of primary gas in the first zone is very easy to vary across a wide range.
  • waste gases from gas burners, gas-driven boilers, gas motors or gas turbines are used for example.
  • gas motors on the basis of available waste gas such as the biological gas that results from fermentation produced by purifying sewage water, for example. Because in this case the heat from the waste gases from the motor are also used efficiently, the efficiency increases significantly compared to the conventional separate set-up of the bio-gas motor wherein only the generated electricity and heat from the cooling water is used.
  • the waste gases arising from this can be mixed with air from the outside in order to achieve the required temperature combined with the required oxygen percentage, wherein a certain percentage of oxygen is still added to these gases.
  • the amount of air that is added to the waste gases from the outside depends on the temperature that is necessary for the primary gas in the first zone. In general this will be from 100°C to 270°C.
  • the oxygen percentage in this case will be from 0 % to 15 %.
  • the recovery of the heat from the burning of the gas in the gas boiler will result in a higher efficiency for the entire installation.
  • Waste gas from a gas turbine can also be used in a suitable way. Especially in the case of waste gases from a gas turbine or gas motor, these can have a temperature higher than 270°C, for example 450°C or higher. If the waste contains some humidity and the flow in the first primary zone is not too high, even with these temperatures the pyrolisis may be limited so that sufficient caloric value remains in the waste, so as to get a good combustion in the successive (second) zone. Mixing with cool air or cooler recirculation waste gas is possible as well. The invention is therefore also adaptable for similar cases wherein the temperature of the primary gas supply is higher than 300°C.
  • the waste gases from the waste incinerator as shown in the figure, which are extracted after they have passed through the dust filter (11), are at a temperature of from 100°C to 270°C.
  • a problem that can occur using similar waste gas recirculation is corrosion at 'cold spots' and the leaking of the recirculation gases to the outside in places where high pressure is present. Because of the temperature of the recirculation gases, similar corrosion is possible as the result of condensation of the recirculating gas in the pipes supplying gas to the incineration zone, for example underneath the incinerator grid (5).
  • any leakage of the recirculating gases in this housing (12) will not lead to direct problems in the surrounding area because the leaked gases will be taken up and diluted in the housing (12). These gases can then be passed on to the incineration zone.
  • the second part of the supply of the primary gas is used to maintain the surroundings of the supply of the first part of the gas supply (1) at the required, higher, temperature so that no condensation can take place.
  • the supply (1), and especially the funnel under the grid (5) for the first zone, as shown in Figure 2 are situated in this case in a casing (12) which is kept at a temperature that is regulated by the second part of the gas supply, and which can also be kept at a higher pressure according to a further recommended implementation.
  • this supply of the first part of the gas is insulated and surrounded by the air pre-heated by an air pre-heater, cold bridges can be prevented by this construction.
  • this air-preheater is the heater of the second part of the primary gas supply (7) this heater should work continuously at a sufficiently high temperature. If necessary, a bypass can be provided in this case wherein the primary gas that is supplied to the second zone does not pass through the air pre-heater (7). It is also possible, using a control valve, to provide a connection between the pre-heated air coming from the housing and the funnel for the first part of the gas supply in order to add oxygen-rich air to the first part of the supply.
  • the waste gas that is used for recirculation should preferably be withdrawn from the waste incinerator via a baghouse filter or electrostatic filter (11), so that the amount of dust in the recirculating gas is low and no problems arise with deposits occurring in the pipes.
  • the temperature of the recirculation gas is from 170°C to 270°C, preferably in the area of 190°C and 230°C. This temperature must be high enough to prevent problems with the condensation of the waste gases, but also low enough for it to be treated by common baghouse filter materials, for example a special catalytic layer on the baghouse filter material.
  • the primary air for the first zone is regulated in order to control the fire in the second and third zones.
  • the range of the gas supply via the first zone must be approximately 2.5% to 25% of the total amount of primary gas.
  • 10% of the total is enough to dry the waste material well, through the high temperature of the recirculation gases used.
  • the drying process is more than good and the amount of the gas supply can be reduced to 5%.
  • the amount can be increased to 20%.
  • the incinerator grid (5) in the first zone, on which the waste material to be burnt (6) is initially placed does not have to be equipped with water cooling.
  • condensation of water from the recirculated gas can especially occur on the cooled parts.
  • the recirculation gases have a very low oxygen content but a relatively high temperature, so that virtually no combustion takes place in the waste material above the first zone.
  • flame temperatures can exist of up to a maximum of 500°C if the oxygen content is lower than 10% by volume. Because of the low oxygen content and the low temperature, the flame front can however hardly creep downwards. This means that damage to the incinerator grid (5) in the first zone by overheating of the grid cannot occur.
  • the waste material from the first zone that reaches the second zone is, however, very well dried and easily combustible.
  • a primary air supply is added with a normal oxygen content. This causes the flame front to move downwards virtually instantaneously.
  • the incinerator grid in the second zone (5) is water-cooled. Because of the oxygen content as well as the good mix of the oxygen and the waste material to be burned, a very fierce fire will occur in the incinerator bed that burns right up to the grid (5).
  • the very easily combustible parts of the waste material (especially synthetic materials) already lose part of their thermal values and the peak temperatures in the second and third zones are lower than in the case where the waste material in the first zone is completely incinerated, as is the usual case when oxygen-rich air is used.
  • the heat that the grid (5) absorbs and gives off to the cooling water is re-used in a suitable way.
  • the primary gas for the second and third zones can be used without any further air pre-heating (7, 8), thereby lowering grid and flame temperature as well as reducing NO x formation.
  • the gas that is supplied to the second and third zones can therefore be fresh air that can be supplied directly from the outside.
  • the energy saving that is achieved by this it has the advantage that when the air is cold, the air speed will be lower for an equal supply of oxygen, wherein less flue dust will be created.
  • the amount of oxygen that is supplied via the second and third zones to the waste material that is to be burnt (6) must be approximately stoichiometric or somewhat less (from 0.8 to 1.0 times the amount of oxygen necessary for the combustion).
  • the amount of air that is supplied to the second and third zones is approximately from 25% to 30% of the total amount of gas that is used as the primary and third air supply. The result of this is that the highest heat develops in the waste bed itself.
  • the coal residue that is to say the percentage of unburned carbon
  • the quality of the resulting slag is therefore improved on account of the good drying in the first zone.
  • the gas that is used for the second and third zones should preferably not be pre-heated, and in the case of a good enough supply of waste material that can therefore be pre-dried in order to achieve a rapid combustion in the second zone, an air pre-heater (7, 8) can be omitted if required.
  • the last zone is a final incineration and cooling zone that only receives from 5% to 15% of the total amount of gas.
  • Recirculated gas can possibly be used here. This has the advantage that the CO 2 and H 2 O contained in the recirculated gas, if necessary supplemented with extra water, reacts with the calcium in the slag, wherein this goes through a rapid ageing process and there exists a lower pH value in any later leaching. In this way the quality of the slag is improved because there is less leaching.
  • the incineration in the main incineration zone is not going very well it can be useful to temporarily use an increased oxygen content directly after the main incineration zone in order to bring about a good combustion of the lower ash layer.
  • recirculated gas that is to say waste gas from the incinerator
  • the preference is the percentage is from 5% to 30% of the total amount of air supplied, preferably from 10% to 20%.
  • waste transport As the primary regulator for the capacity of the plant.
  • the supply of waste material to the grid must be adjusted in order to obtain a good layer thickness.
  • the individual regulating of the temperature in each zone proposed in Claim 2 it is possible to temporarily support a local lack of combustion in the main combustion zone without adapting the amount of the air supply.
  • the limiting of the formation of NO x and the negative influence on the waste throughput aim to keep the nominal air temperature in the main combustion zone as low as possible. This can be controlled by influencing the drying process in the first zone. For this a fixed, as low as possible, oxygen percentage is aimed for in principle, and a high temperature in the first primary gas supply. In this way the first primary gas supply becomes the primary regulating quantity for the drying of the waste material. This flow is regulated such that a good combustion takes place in the second zone, but not more than what is needed to prevent too fierce combustion.
  • the invention provides a much-improved technique for burning waste material in a waste incinerator.
  • the extra investments that are necessary for the recirculation of the waste gas and the more complex construction for the supply of the recirculation gases to the first zone are compensated for by the fact that the waste gas cleaning can be carried out on a smaller scale, and the fact that a lot less energy is needed for the preheating of the primary part of the gas supply.
  • the advantages are especially achieved because the incineration is better and because this results in an ash layer of a better quality.
  • waste material with a wide range of thermal values from 5,000 to 16,000 kilojoules per kilogram

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Incineration Of Waste (AREA)

Claims (18)

  1. Procédé d'incinération de matériaux de rebut dans un incinérateur, qui comprend :
    - l'approvisionnement en matériau de rebut à une zone d'incinération qui contient une grille d'incinération, dans laquelle le matériau de rebut est fourni à une première face de la grille d'incinération et est transféré sur une seconde face pendant le processus.
    - l'approvisionnement à partir d'en dessous à travers la grille d'incinération et le matériau de rebut placé au dessus, au gaz primaire de façon à incinérer au moins partiellement le dit matériau de rebut dans une zone de combustion qui s'étend de la grille d'incinération vers un premier niveau au dessus de la grille d'incinération, dans lequel la zone d'incinération comprend au moins deux zones, le matériau de rebut étant fourni à une première zone et dans laquelle pendant le processus, le matériau de rebut est déplacé vers une zone reliée consécutive ; un premier gaz partiel primaire est fourni à la première zone ayant une teneur en oxygène de moins de 20 % en volume et une température allant de 50°C à 450°C, de préférence de 50°C à 300°C, et un gaz primaire partiel consécutif est fourni à au moins la zone consécutive.
    et
    caractérisé en ce que la température est contrôlée pour chaque alimentation en gaz primaire partiel.
  2. Procédé selon la revendication 1 caractérisé en ce que l'alimentation en premier gaz primaire partiel comprend du gaz de rebut provenant d'un incinérateur, de préférence du gaz de rebut provenant d'un incinérateur de rebuts, une chaudière à gaz, un moteur à gaz ou une turbine à gaz, du gaz de rebuts provenant d'un incinérateur de déchets étant davantage préféré.
  3. Procédé selon la revendication 1 ou la revendication 2 caractérisé en ce que la construction de l'alimentation de la fourniture en premier gaz primaire partiel, pour autant que celui-ci comprend du gaz de rebut provenant d'un incinérateur, est enfermée dans un coffrage, le dit coffrage étant alimenté par des gaz à des températures et/ou à des pressions égales à ou supérieures à la température ou à la pression respectivement de la première alimentation en gaz primaire.
  4. Procédé selon la revendication 2 ou la revendication 3 caractérisé en ce que le gaz de rebuts provenant d'un incinérateur, est filtré, de préférence à travers un filtre à poussières.
  5. Procédé selon la revendication 1 à 4, caractérisé en ce que du gaz secondaire est fourni près du premier niveau au-dessus de la grille d'incinération et un troisième gaz est fourni à un second niveau au-dessus du premier niveau, pour lequel le gaz secondaire possède une teneur en oxygène de < 20 % en volume et le troisième gaz a une teneur en oxygène plus élevée que celle du gaz secondaire.
  6. Procédé selon la revendication 5, caractérisé en ce que le gaz secondaire contient des gaz de rebuts provenant d'un incinérateur de déchets.
  7. Procédé selon la revendication 5 ou la revendication 6 caractérisé en ce que le troisième gaz contient de l'air de l'extérieur.
  8. Procédé selon la revendication 1 à 7, caractérisé en ce que le gaz primaire dans la première zone possède une teneur en oxygène allant de 0 à 15 % -de préférence de 0 à 10 %.
  9. Procédé selon la revendication 1 à 8, caractérisé en ce que le gaz primaire est alimenté par au moins trois alimentations partielles dans lesquelles au moins :
    - une première alimentation en gaz partielle possède une teneur en O2 allant de 0 % à 15 % et représente de 2 à 25 % de la quantité totale de gaz primaire ;
    - un ou plusieurs alimentations en gaz successives partielles constituant de 15 à 90 % de la quantité totale de gaz primaire ;
    - une dernière alimentation en gaz partielle constituant de 5 à 25 % de la quantité totale de gaz primaire.
  10. Un procédé selon la revendication 1 à 9, caractérisé en ce que le coffrage est garni avec du gaz provenant d'une alimentation en gaz primaire partielle consécutive.
  11. Procédé selon la revendication 10, caractérisé en ce que les gaz provenant du coffrage sont ensuite fournis à la zone d'incinération, par exemple en les mélangeant avec la première alimentation en gaz primaire partiel.
  12. Procédé selon la revendication 10, caractérisé en ce que les gaz provenant du coffrage sont ensuite fournis à une zone d'incinération successive, par exemple par l'intermédiaire d'une paroi latérale ou en tant que gaz secondaire dans la chaudière en tant que gaz d'incinération.
  13. Procédé selon les revendications 10 à 12, caractérisé en ce que le coffrage est alimenté avec des gaz à une température d'au moins 150°C.
  14. Procédé selon les revendications 1 à 13, caractérisé en ce que le tube pour l'alimentation des gaz de recirculation est inclus dans un tube qui est alimenté en gaz à une température et/ou à une pression égale à ou supérieure à celle de la première alimentation en gaz partielle primaire.
  15. Procédé selon les revendications 1 à 14, caractérisé en ce que la première alimentation en gaz partielle primaire est régulée de façon à exercer une influence sur l'incinération dans la zone d'incinération principale connectée, en variant principalement le flux de la première alimentation en gaz partielle primaire, et la teneur en oxygène et/ou la température est ensuite ou en même temps variée.
  16. Four d'incinération pour les déchets destiné à un incinérateur de déchets, qui consiste en une grille d'incinérateur (8) pour les matériaux de déchets (4) qui doivent être incinérés, des moyens pour déplacer les déchets qui doivent être incinérés en partant d'un premier côté vers un second côté, des moyens d'alimentation en gaz primaire (1,2,3,4) sous la grille de l'incinérateur, des moyens d'alimentation (9) en gaz secondaire à un premier niveau au dessus de la grille d'incinérateur et des moyens d'alimentation en gaz tertiaire (10) à un second niveau au dessus de la grille de l'incinérateur et au dessus des moyens d'alimentation en gaz secondaire dans lequel les moyens d'alimentation en gaz secondaire sont reliés à un échappement de gaz de déchet provenant de l'incinérateur de déchets caractérisé en ce qu'un détecteur de température et un réchauffeur sont disposés pour la commande de chaque température d'alimentation en gaz primaire.
  17. Four d'incinération de déchets selon la revendication 16, caractérisé en ce que les moyens d'alimentation en gaz primaire, sont reliés à un échappement de gaz de déchet à partir d'un brûleur à gaz, une chaudière de gaz, un moteur à gaz, une turbine à gaz, une installation de fermentation à eau pour eaux d'égout ou un moteur à bio gaz.
  18. Four d'incinération pour déchets selon la revendication 16, caractérisé en ce que les moyens d'alimentation en gaz primaire consistent en au moins deux alimentations séparées, le premier moyen d'alimentation en gaz primaire étant placé près du premier côté sous la grille d'incinérateur et le second moyen d'alimentation en gaz primaire étant placé près du second côté sous la grille d'incinérateur et le premier moyen d'alimentation en gaz primaire étant connecté à un échappement de gaz de déchets provenant d'un incinérateur pour déchets.
EP01202285A 2000-06-14 2001-06-14 Recirculation des gaz de combustion d'un incinérateur d'ordures Expired - Lifetime EP1164331B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL1015519 2000-06-14
NL1015519A NL1015519C2 (nl) 2000-06-14 2000-06-14 Rookgasrecirculatie bij een afvalverbrandingsinstallatie.

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EP1164331A1 EP1164331A1 (fr) 2001-12-19
EP1164331B1 true EP1164331B1 (fr) 2006-09-06

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EP (1) EP1164331B1 (fr)
AT (1) ATE338917T1 (fr)
CY (1) CY1105828T1 (fr)
DE (1) DE60122829T2 (fr)
DK (1) DK1164331T3 (fr)
ES (1) ES2272406T3 (fr)
NL (1) NL1015519C2 (fr)
PT (1) PT1164331E (fr)

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CN105351944A (zh) * 2015-12-10 2016-02-24 重庆三峰卡万塔环境产业有限公司 一种改进的炉排炉垃圾焚烧装置

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US6497187B2 (en) * 2001-03-16 2002-12-24 Gas Technology Institute Advanced NOX reduction for boilers
AT412500B (de) * 2002-10-29 2005-03-25 Wilde Andreas Ing Verfahren zum verbrennen von kleinstückeligem brennstoff
US7146916B2 (en) * 2004-05-14 2006-12-12 Eco/Technologies, Llc Starved air inclined hearth combustor
DE102006005464B3 (de) 2006-02-07 2007-07-05 Forschungszentrum Karlsruhe Gmbh Verfahren zur primärseitigen Stickoxidminderung in einem zweistufigen Verbrennungsprozess
DE102009014010B4 (de) * 2009-03-19 2012-02-23 Georg Fischer Gmbh & Co. Kg Brenner für festes, stückiges Brennmaterial
EP2505919A1 (fr) * 2011-03-29 2012-10-03 Hitachi Zosen Inova AG Procédé d'optimisation de la combustion des gaz d'échappement d'une installation de combustion par homogénéisation des gaz de fumée dessus du lit de combustion réalisée par injection des gaz de fumée
JP5871207B2 (ja) * 2012-06-12 2016-03-01 Jfeエンジニアリング株式会社 廃棄物焼却炉及び廃棄物焼却方法
JP6260058B2 (ja) * 2014-09-12 2018-01-17 三菱重工環境・化学エンジニアリング株式会社 ストーカ式焼却炉
CN107631301A (zh) * 2016-08-01 2018-01-26 北京北控环保工程技术有限公司 立式焚烧炉及危废物分区焚烧系统
DE102017008123A1 (de) * 2017-08-30 2019-02-28 Martin GmbH für Umwelt- und Energietechnik Feuerungsanlage und Verfahren zum Betreiben einer Feuerungsanlage
CN112783236B (zh) * 2019-11-11 2022-06-14 株式会社盖亚 一种用于烘干机的自动冷却切换的烘干控制方法
JP7051792B2 (ja) * 2019-12-18 2022-04-11 三菱重工業株式会社 燃焼設備の状態特定装置、状態特定方法およびプログラム
CN113406282B (zh) * 2021-06-18 2022-08-30 国网安徽省电力有限公司电力科学研究院 电站锅炉尾部烟道氧量场标定方法

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JPH0247648B2 (ja) * 1984-12-17 1990-10-22 Hitachi Shipbuilding Eng Co Nenshohaigasuomochiitaboirachuubunofushokuboshihoho
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CN105351944A (zh) * 2015-12-10 2016-02-24 重庆三峰卡万塔环境产业有限公司 一种改进的炉排炉垃圾焚烧装置

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NL1015519C2 (nl) 2001-12-28
CY1105828T1 (el) 2011-02-02
DK1164331T3 (da) 2007-01-02
ES2272406T3 (es) 2007-05-01
EP1164331A1 (fr) 2001-12-19
DE60122829D1 (de) 2006-10-19
ATE338917T1 (de) 2006-09-15
DE60122829T2 (de) 2007-03-15
PT1164331E (pt) 2007-01-31

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