EP2878887B1 - Procédé de fonctionnement d'une installation d'oxydation de gaz - Google Patents

Procédé de fonctionnement d'une installation d'oxydation de gaz Download PDF

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Publication number
EP2878887B1
EP2878887B1 EP14192777.2A EP14192777A EP2878887B1 EP 2878887 B1 EP2878887 B1 EP 2878887B1 EP 14192777 A EP14192777 A EP 14192777A EP 2878887 B1 EP2878887 B1 EP 2878887B1
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EP
European Patent Office
Prior art keywords
combustion chamber
volumetric flow
heat storage
channel
gas
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Revoked
Application number
EP14192777.2A
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German (de)
English (en)
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EP2878887A1 (fr
Inventor
Stefan Gores
Christoph Dötsch
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Krantz GmbH
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Krantz GmbH
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
    • F23G7/065—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel
    • F23G7/066—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel preheating the waste gas by the heat of the combustion, e.g. recuperation type incinerator
    • F23G7/068—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel preheating the waste gas by the heat of the combustion, e.g. recuperation type incinerator using regenerative heat recovery means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2203/00—Flame cooling methods otherwise than by staging or recirculation
    • F23C2203/30—Injection of tempering fluids

Definitions

  • the heat storage masses are usually arranged in separate containers or in a common container divided by partitions, and a raw gas volume flow and a clean gas volume flow flow through them alternately.
  • the heat storage masses can be divided into an upper area facing the combustion chamber and a lower area facing away from the combustion chamber.
  • the heat storage masses arranged in a container can also be understood as a single heat storage mass, which is divided into two sections, if necessary by means of a partition wall, with each section being flowed through alternately by the raw gas volume flow and the clean gas volume flow.
  • a raw gas duct and a clean gas duct lead to the individual heat storage masses, with the raw gas volume flow or the clean gas volume flow being alternately passed through the corresponding heat storage mass depending on the process cycle.
  • the first heat storage mass preheats the raw gas volume flow before the latter is directed into the combustion chamber and there through the Oxidation of the oxidizable components is converted into the clean gas volume flow.
  • the clean gas volume flow transfers its thermal energy to the second downstream heat storage mass.
  • the raw gas volume flow first flows through the second heat storage mass, previously preheated by the clean gas volume flow, and heats the latter.
  • the clean gas volume flow is now passed through the first heat storage mass through which the raw gas volume flow previously flowed, the latter now heating up the first, now “downstream” heat storage mass.
  • a bypass such as this one in the DE 10 2010 012 005 A1 is described, connected to the combustion chamber.
  • the clean gas volume flow is derived directly from the combustion chamber and consequently a certain amount of thermal energy is withdrawn from the gas oxidation system.
  • a total failure of the gas oxidation plant can already have occurred within this period. This means that the bypass is only an influencing factor on the system temperature that has a very sluggish effect.
  • bypass Another disadvantage of the bypass is that it is difficult to estimate how much thermal energy has to be diverted via the bypass. It may well be possible that so much thermal energy is unintentionally dissipated that the raw gas volume flow is not sufficiently preheated by the upstream heat storage mass. In this case, the heat source does not manage to heat up the insufficiently preheated raw gas volume flow in such a way that sufficient oxidation of the oxidizable components in the raw gas volume flow occurs. This can result in the required clean gas limit values no longer being met.
  • the object of the present invention is to further develop a device and a method such that the gas oxidation system can be cooled down with as little delay as possible in order to prevent a total failure of the system.
  • the energy generated in the gas oxidation plant should be used as efficiently as possible without exceeding the clean gas limit values.
  • the underlying object is achieved by at least one channel which is preferably connected directly to the combustion chamber and by means of which a fluid can be introduced into the combustion chamber, with the introduction of the fluid leading to a temperature reduction in the combustion chamber .
  • the combustion chamber temperature can be lowered immediately after detecting an excessive temperature rise in the combustion chamber by introducing the fluid into the combustion chamber and mixing it with the gas mixture therein. It can even be compensated for suddenly occurring temperature increases within the heat storage mass. It is therefore a manipulated variable that acts very quickly on the combustion chamber temperature.
  • the temperature increases are due to changes in the energy content or increases in the concentration of the oxidizable components in the raw gas volume flow, since these lead to an increased exothermic reaction and thus to an increased release of thermal energy.
  • the supplied fluid has the lowest possible temperature, at least well below the combustion chamber temperature, with a fluid at ambient or room temperature usually being used.
  • the heat loss within the gas oxidation system can be kept as low as possible, since the thermal energy, in contrast to the devices and operating methods known from the prior art, is at least not dissipated via a thermally unused bypass flow, but within the Gas oxidation system, and although primarily remains in the heat storage masses.
  • the fact that a total failure of the gas oxidation system can nevertheless be avoided can be explained as follows:
  • the introduction of a sufficiently cool fluid into the combustion chamber has a very immediate and timely effect, i.e. a reduction in the combustion chamber temperature, which in particular avoids a system shutdown due to overheating if the temperature sensors that could trigger a possible shutdown are located in the combustion chamber, which according to the technology is common.
  • the method according to the invention can be assessed as very positive from the point of view of energy efficiency, since, despite the cooling effect, no energy is released unused from the system (as is the case with a bypass without heat recovery), but rather the energy in the heat storage mass downstream of the combustion chamber is (temporarily) stored. This is particularly useful if the overheating problem is only caused for a short period of time due to a temporary peak in the content of oxidizable components in the raw gas and this peak would soon be replaced by phases in which (just) autothermal operation would be possible or there is even a sub-autothermal operating state again.
  • the introduction of fluid into the combustion chamber according to the invention also offers a very elegant possibility for regulating the temperature level of the heat storage masses. Even without a concrete reason for a temperature reduction in the combustion chamber, it can make sense to introduce fluid there, if the temperature within the heat storage masses drops so much as a result of prolonged use of a hot bypass that insufficient preheating of the raw gas volume flow leads to the clean gas limit values being exceeded .
  • a higher volume flow is passed through the second heat storage mass to be heated, so that the temperature within this mass and through the cyclic switching of the flow direction is raised by the temperature of the entire heat storage mass.
  • the fluid is formed by outside air.
  • a gaseous state of the fluid enables particularly good mixing of the fluid with the gas mixture in the combustion chamber.
  • the fluid is formed from the outside air, no additional fluid arranged in containers, for example, has to be kept ready.
  • the fluid from a liquid, in particular water or an aqueous liquid is formed. In this case, the cooling effect is intensified by the vaporization enthalpy of the water.
  • this embodiment is not part of the invention.
  • a particularly advantageous embodiment of the invention provides that the at least one channel opens into at least one, preferably two, feed points, with the feed points preferably being located in an upper area of the combustion chamber.
  • the mixing of the fluid and the gas mixture takes place at different locations due to the plurality of feed points, as a result of which the most rapid and uniform possible mixing is achieved.
  • the arrangement of the feed points in the upper part of the combustion chamber i.e. the area of the combustion chamber that is not located directly on the at least one heat storage mass, promotes good mixing of the fluid with the gas mixture, in that the fluid flows through the warm, in the combustion chamber gas mixture that has risen above cools immediately.
  • the "cooler" gas mixture is in the area of the combustion chamber that borders on the heat storage masses. This means that the gas mixture, which has a lower temperature, comes into contact with the heat storage mass and heats it up. Since the temperature of the gas mixture is within a tolerable range, the heat storage mass is heated to a lesser extent because of the dependency.
  • the fluid is at least partially formed by the clean gas volume flow.
  • the clean gas volume flow that is already available only needs to be conducted directly or indirectly into the combustion chamber by means of the channel. As a result, no further fluid needs to be kept ready. Furthermore, any oxidizable components still present in the clean gas volume flow are heated again and cleaned by oxidation. This makes it possible to improve the clean gas values with regard to the residual pollutant content.
  • this embodiment is not part of the invention.
  • the at least one channel is connected directly to the clean gas channel.
  • the channel preferably leads to the at least one feed point in the combustion chamber. A conversion of existing gas oxidation plants is easily possible.
  • a burner is arranged in the combustion chamber, with a combustion air duct of the burner preferably forming the at least one duct.
  • the type of arrangement does not require any additional conversion work, since the combustion air duct, which directs air for combustion into the combustion chamber, already exists is available.
  • the burner also has a fuel duct for introducing a fuel into the combustion chamber.
  • the at least one duct can optionally also be arranged between the clean gas duct and the combustion air duct. Any complications arising from the dual use of a section of the combustion channel do not exist since the fluid is only fed into the combustion chamber when the temperature is too high. When the burner is used, on the other hand, there is just not enough thermal energy in the combustion chamber due to the exothermic reaction. Consequently, no fluid needs to be introduced into the combustion chamber in order to cool the gas mixture.
  • an advantageous embodiment of the invention provides at least one additional duct which is directly connected to the combustion chamber is connected, by means of this channel, the fluid, preferably outside air, can be introduced into the combustion chamber.
  • the fluid preferably outside air
  • the proportion of the volume flow of the fluid introduced into the combustion chamber in relation to the raw gas volume flow should be between 1% and 25%, preferably between 5% and 15%.
  • the at least one further channel can be connected directly to the clean gas channel or is formed by the combustion air channel. This constructive conversion work can be managed without any problems. It can also be provided that the first duct is connected to the clean gas duct and the further duct is formed by the combustion air duct. A reverse arrangement is also conceivable.
  • a bypass duct is fluidically connected to the combustion chamber, preferably directly, with the bypass duct preferably having a heat exchanger device.
  • Thermal energy can be removed from the gas oxidation plant by means of the bypass in order to use it for other purposes, e.g. B. to generate steam, to use thermal oil, hot water or hot air.
  • the bypass results in additional cooling of the gas oxidation system or the heat storage masses.
  • At least one additional channel is connected to the gas oxidation system in such a way that the fluid introduced into the gas oxidation system by means of the additional channel can be mixed with the raw gas volume flow before a mixed volume flow formed by the raw gas volume flow and the fluid in one of the heat storage masses occurs.
  • Mixing the fluid with the raw gas volume flow before the latter is introduced into the upstream heat storage mass reduces the concentration of oxidizable components in the raw gas volume flow. This can prevent an over-autothermal reaction from occurring and the temperature in the combustion chamber and the heat storage masses from rising uncontrollably. If the temperature should nevertheless rise, this can be compensated for again by means of the channels that introduce fluid into the combustion chamber.
  • the further channel is connected directly to the at least one raw gas channel.
  • a fluid is introduced directly into the combustion chamber by means of at least one channel.
  • the fluid mixes with the gas mixture, which consists partly of the raw gas volume flow and partly of the clean gas volume flow.
  • the outside air is fed into the combustion chamber as a fluid at at least two feed points. This results in the advantage that if one of the feed points fails, another feed point is still available. If there are at least two feed points on the combustion chamber, this leads to particularly good mixing of the gas mixture and the fluid.
  • the aforementioned configuration is particularly advantageous if the fluid is introduced into the combustion chamber starting from the clean gas duct and/or the fluid is conducted into the combustion chamber through a combustion air duct of a burner. Structurally, this arrangement can be easily achieved since the combustion air duct and an associated feed point are already present and only the fluid has to be routed through the duct. If the fluid is formed, preferably additionally, by the clean gas, the channel leads from the clean gas channel to the feed point.
  • At least part of the clean gas volume flow is discharged via a bypass.
  • the thermal energy that is produced in the gas oxidation system can be diverted via the bypass and, for example, by means of a heat exchanger for use by others place (heating, process heat, etc.) are decoupled.
  • the raw gas volume flow is mixed with the fluid, so that a mixed volume flow is formed before the mixed volume flow in one of the
  • Heat storage masses is conducted. In this way, the concentration of oxidizable components in the raw gas volume flow can be reduced before it is passed through the upstream heat storage mass, so that less thermal energy is released in the system.
  • the figure 1 shows a circuit diagram of a gas oxidation system 101 with a first heat storage mass 2 and a second heat storage mass 3.
  • the heat storage masses 2 , 3 are each arranged in a container 4 , 5 , with heat storage masses 2 , 3 each having a raw gas channel 6 and a clean gas channel 7 are connected. It is provided that both the raw gas channel 6 and the clean gas channel 7 can be fluidically separated from the containers 4 , 5 by means of valves 8 , 9 , 10 , 11 .
  • the two heat storage masses 2 , 3 are connected to one another via a combustion chamber 12 .
  • a burner 13 is located in the combustion chamber 12 as an external heat source. Even if it is quite common to use a burner 13 in gas oxidation systems 101 , gas oxidation systems without burners 13 are also conceivable in certain constellations.
  • the first valve 8 is opened and the second valve 9 is closed so that a raw gas volume flow can be introduced via the raw gas channel 6 into a lower region 14 of the first heat storage mass 2 .
  • the lower region 14 of the heat storage masses 2 , 3 is a part of the heat storage masses 2 , 3 which faces away from the combustion chamber 12 and is therefore the first to come into contact with the raw gas volume flow.
  • An upper area 15 of the heat storage masses 2 , 3 faces the combustion chamber 12 .
  • the second valve 9 which is closed in this process cycle, prevents the raw gas volume flow from entering the clean gas channel 7 . That means for this one Process cycle that the first heat storage mass 2 is connected in front of the combustion chamber 12 .
  • the raw gas volume flow is heated by the first upstream heat storage mass 2 before it is conducted further into the combustion chamber 12 . Subsequently, the crude gas volume flow within the combustion chamber 12 is further heated by the burner 13 , as a result of which the oxidizable components present in the crude gas volume flow oxidize and thermal energy is released. This process converts the raw gas volume flow into a clean gas volume flow. Thermal energy is required to initiate and possibly also maintain the oxidation (endothermic), but thermal energy is also released by the oxidation (exothermic).
  • the oxidation of the oxidizable components takes place both in the combustion chamber 12 and in the second heat storage mass 3 , which is connected downstream of the combustion chamber 12 .
  • the combustion chamber 12 there is a gas mixture which consists partly of the raw gas volume flow and partly of the clean gas volume.
  • the thermal energy produced during the oxidation is released to the second heat storage mass 3 .
  • the clean gas volume flow leaves the second heat storage mass 3 via the clean gas channel 7.
  • the third closed valve 10 in this process cycle prevents the crude gas volume flow from flowing through the second downstream heat storage mass 3 .
  • the fourth valve 11 is open and connects the second downstream heat storage mass 3 to the clean gas channel 7.
  • the fourth valve 11 is closed and the third valve 10 is opened.
  • the raw gas volume flow is heated with the thermal energy stored in the second heat storage mass 3 before it is conducted into the combustion chamber 12 .
  • the raw gas volume flow is further heated so that the oxidation can take place.
  • the resulting clean gas volume flow is conducted into the first heat storage mass 2 and releases its thermal energy there.
  • the exothermic reaction releases more thermal energy than would be acceptable in the stationary state for compliance with certain maximum temperatures.
  • the temperature inside the combustion chamber 12 and also in the respective downstream heat storage mass 2 , 3 rises sharply.
  • the gas mixture is mixed with a fluid.
  • the fluid is introduced via a channel 16 which is connected to the combustion chamber 12 at a feed point.
  • the supply of the fluid is controlled via a fifth valve 17 .
  • the feed point is preferably located in an upper part of the combustion chamber 12 facing away from the heat storage masses 2 , 3.
  • the fluid is formed from outside air.
  • an air conveying device that may be required in the channel 16 is not shown in the drawing.
  • FIG. 1 Another possible embodiment is dashed in the figure 1 shown. This shows that there can also be several feed points on the combustion chamber 12 , it being conceivable that further channels 18 lead to the respective feed points or that the channel 16 has branches to the various feed points.
  • the figure 2 shows an alternative embodiment of the gas oxidation system 201 according to the invention.
  • the channel 16 is arranged between the clean gas channel 7 and the feed point in the combustion chamber 12 . This means that the fluid is formed by the clean gas volume flow.
  • FIG 3 a further gas oxidation system 301 according to the invention is shown, with the gas oxidation system 301 being different from the gas oxidation system 101 in figure 1 differs in that the channel 16 is not arranged between the clean gas channel 7 and the combustion chamber 12 , but is formed by a combustion air channel 19 of the burner 13 .
  • the duct 16 can connect the clean gas duct 7 to the combustion air duct 19 of the burner 13 and thus introduce the clean gas volume flow into the combustion chamber 12 as a fluid.
  • the figure 4 shows an example of how figure 1 , with a bypass channel 20 and/or another channel 21 also being connected to the gas oxidation system 401 .
  • the bypass channel 20 directs part of the clean gas volume flow directly out of the combustion chamber 12 .
  • the thermal energy is extracted via a heat exchanger device 22 , which the bypass channel 20 has, and used in some other way.
  • the further channel 21 directs the fluid into the raw gas channel 6 in order to mix the raw gas volume flow with the fluid before this mixed volume flow thus formed is passed into the upstream heat storage mass.

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

Claims (9)

  1. Procédé de réduction de la température de chambre de combustion lors du fonctionnement d'une installation d'oxydation gazeuse (101, 201, 301, 401) pour le traitement thermique d'un débit volumique de gaz brut chargé de composants oxydables, comprenant les étapes opératoires suivantes :
    a) Le débit volumique de gaz brut est conduit à travers au moins une masse d'accumulation thermique installée en amont (2, 3) vers une chambre de combustion (12), de l'énergie thermique accumulée dans cette masse d'accumulation thermique (2, 3) étant transférée dans le débit volumique de gaz brut et le réchauffant.
    b) Dans la chambre de combustion (12), les composants du débit volumique de gaz brut sont oxydés et le débit volumique de gaz brut est ainsi transformé en un débit volumique de gaz pur.
    c) En partant de la chambre de combustion (12), le débit volumique de gaz pur est conduit au moins partiellement et/ou temporairement dans au moins une masse d'accumulation thermique installée en aval (2, 3), de l'énergie thermique contenue dans le débit volumique de gaz pur étant transférée dans cette masse d'accumulation thermique installée en aval (2, 3) et la réchauffant.
    d) Le débit volumique de gaz pur est conduit dans un canal à gaz pur (7),
    caractérisé par l'étape opératoire suivante :
    e) en cours de fonctionnement de l'installation d'oxydation gazeuse (101, 201, 301, 401), pour une partie de composants oxydables dans le débit volumique de gaz brut, par laquelle partie, suite à une réaction exothermique, plus d'énergie thermique a été dégagée qu'il ne serait acceptable en fonctionnement stationnaire de l'installation d'oxydation gazeuse pour le maintien de certaines températures maximales, de l'air extérieur est conduit au moyen d'un canal (16) directement dans la chambre de combustion (12), ce qui fait baisser la température de la chambre de combustion et empêche une coupure de l'installation en raison d'une température excessive.
  2. Procédé selon la revendication 1, caractérisé en ce que l'air extérieur est conduit vers au moins deux points d'alimentation, se trouvant de préférence dans une partie supérieure de la chambre de combustion, dans la chambre de combustion (12).
  3. Procédé selon la revendication 1 ou 2, caractérisé en ce que l'air extérieur est conduit à travers un canal d'air de combustion (19) d'un brûleur (13) dans la chambre de combustion (12).
  4. Procédé selon une des revendications 1 à 3, caractérisé en ce qu'au moins une partie du débit volumique de gaz pur est évacuée par un canal de contournement (20).
  5. Procédé selon une des revendications 1 à 4, caractérisé en ce que le débit volumique de gaz brut est mélangé avec de l'air extérieur, de sorte qu'il est constitué un débit volumique mixte avant que le débit volumique mixte soit conduit dans une masse d'accumulation thermique (2, 3).
  6. Procédé selon une des revendications 1 à 5, caractérisé par au moins un autre canal (18) qui est raccordé directement à la chambre de combustion (12), de l'air extérieur pouvant être conduit dans la chambre de combustion (12) au moyen de ce canal.
  7. Procédé selon une des revendications 1 à 3, caractérisé par un canal de contournement (20) qui est raccordé au niveau de la technique d'écoulement à la chambre de combustion (12), de préférence directement, le canal de contournement (20) présentant de préférence un dispositif échangeur de chaleur (22).
  8. Procédé selon une des revendications 1 à 7, caractérisé par au moins un autre canal (21) qui est raccordé à l'installation d'oxydation gazeuse (101, 201, 301, 401) de manière à ce que l'air extérieur conduit au moyen de l'autre canal (21) dans l'installation d'oxydation gazeuse (101, 201, 301, 401) puisse être mélangé avant qu'un débit volumique mixte constitué du débit volumique de gaz brut et du fluide entre dans une des masses d'accumulation thermique (2, 3).
  9. Procédé selon la revendication 8, caractérisé en ce que l'autre canal (21) est connecté directement à l'au moins un canal à gaz brut (6).
EP14192777.2A 2013-11-27 2014-11-12 Procédé de fonctionnement d'une installation d'oxydation de gaz Revoked EP2878887B1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE102013224297.2A DE102013224297A1 (de) 2013-11-27 2013-11-27 Gasoxidationsanlage sowie Verfahren zu deren Betrieb

Publications (2)

Publication Number Publication Date
EP2878887A1 EP2878887A1 (fr) 2015-06-03
EP2878887B1 true EP2878887B1 (fr) 2022-07-13

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EP14192777.2A Revoked EP2878887B1 (fr) 2013-11-27 2014-11-12 Procédé de fonctionnement d'une installation d'oxydation de gaz

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EP (1) EP2878887B1 (fr)
DE (1) DE102013224297A1 (fr)
PL (1) PL2878887T3 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4470806A (en) * 1982-09-24 1984-09-11 Richard Greco Regenerative incinerators
JP2000088229A (ja) 1998-09-10 2000-03-31 Ishikawajima Harima Heavy Ind Co Ltd アーク炉用排ガス清浄装置
JP2001304531A (ja) 2000-04-26 2001-10-31 Taikisha Ltd 蓄熱型の燃焼式ガス処理装置
JP2007198682A (ja) 2006-01-27 2007-08-09 Takuma Co Ltd 蓄熱脱臭システム
JP2013231552A (ja) 2012-04-27 2013-11-14 Taikisha Ltd 蓄熱式ガス処理装置の運転方法、蓄熱式ガス処理装置、及び、それら運転方法又は蓄熱式ガス処理装置に用いる切換装置

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2624874C2 (de) * 1976-03-30 1984-06-14 Kraftanlagen Ag, 6900 Heidelberg Vorrichtung zur thermischen Nachverbrennung von Prozeßabgasen
US4917027A (en) * 1988-07-15 1990-04-17 Albertson Orris E Sludge incineration in single stage combustor with gas scrubbing followed by afterburning and heat recovery
TW359743B (en) * 1997-01-06 1999-06-01 Nippon Furnace Kogyo Kk Apparatus and method for heating a gaseous fluid flow, method for preheating a gaseous fluid flow
DE102010012005A1 (de) 2010-03-15 2011-09-15 Dürr Systems GmbH Thermische Abluftreinigungsanlage

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4470806A (en) * 1982-09-24 1984-09-11 Richard Greco Regenerative incinerators
JP2000088229A (ja) 1998-09-10 2000-03-31 Ishikawajima Harima Heavy Ind Co Ltd アーク炉用排ガス清浄装置
JP2001304531A (ja) 2000-04-26 2001-10-31 Taikisha Ltd 蓄熱型の燃焼式ガス処理装置
JP2007198682A (ja) 2006-01-27 2007-08-09 Takuma Co Ltd 蓄熱脱臭システム
JP2013231552A (ja) 2012-04-27 2013-11-14 Taikisha Ltd 蓄熱式ガス処理装置の運転方法、蓄熱式ガス処理装置、及び、それら運転方法又は蓄熱式ガス処理装置に用いる切換装置

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PL2878887T3 (pl) 2022-11-21
EP2878887A1 (fr) 2015-06-03
DE102013224297A1 (de) 2015-05-28

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