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WO2009108983A1 - Installation de nettoyage des fumées d’un four - Google Patents

Installation de nettoyage des fumées d’un four Download PDF

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Publication number
WO2009108983A1
WO2009108983A1 PCT/AT2009/000093 AT2009000093W WO2009108983A1 WO 2009108983 A1 WO2009108983 A1 WO 2009108983A1 AT 2009000093 W AT2009000093 W AT 2009000093W WO 2009108983 A1 WO2009108983 A1 WO 2009108983A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
combustion device
flue gases
flue
flue gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/AT2009/000093
Other languages
German (de)
English (en)
Inventor
Anton Secklehner
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.)
Scheuch GmbH
Original Assignee
Scheuch 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
Application filed by Scheuch GmbH filed Critical Scheuch GmbH
Publication of WO2009108983A1 publication Critical patent/WO2009108983A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/364—Avoiding environmental pollution during cement-manufacturing
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • C04B7/47—Cooling ; Waste heat management
    • C04B7/475—Cooling ; Waste heat management using the waste heat, e.g. of the cooled clinker, in an other way than by simple heat exchange in the cement production line, e.g. for generating steam
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0233—Other waste gases from cement factories
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
    • Y02P40/121—Energy efficiency measures, e.g. improving or optimising the production methods

Definitions

  • the invention relates to a system for cleaning the flue gases of a furnace, in particular a cement rotary kiln, with at least one dust separating device which is arranged in the flow direction of the flue gases after the furnace, at least one, the at least one dust separation device downstream supply means for a reducing agent for the reduction of Flue gas contained nitrogen oxides and / or carbon monoxide and / or in particular odoriferous hydrocarbons, and at least one combustion device for • power generation, and a method for cleaning the flue gases of a furnace, in particular a cement rotary kiln, by selective catalytic reduction of nitrogen oxides and / or carbon monoxide and / or especially odoriferous
  • Hydrocarbons with a reducing agent and a reduction catalyst wherein the flue gases are subjected to dedusting before the catalytic reduction.
  • the flue gas denitration is usually carried out by reductive methods.
  • SNCR selective non-catalytic reduction
  • SCR selective catalytic reduction
  • NO x nitrogen oxides
  • a reducing agent - generally ammonia is used as a reducing agent - to elemental nitrogen and water, which subsequently as umweltunbedenkliche substances on the exhaust vent leave the incinerator.
  • the selective non-catalytic reduction is usually carried out at temperatures between 900 0 C and 1100 0 C, wherein the reducing agent is fed directly into the furnace.
  • the selective catalytic reduction can be carried out at significantly lower temperatures, since the catalyst significantly reduces the activation energies required for the reduction reactions.
  • the reducing agent consumption in comparison to SNCR denitrification, in which the reducing agent is used more than stoichiometrically, ver ⁇ be reduced because virtually no side reactions occur.
  • a plant For energy from solid, fossil and particularly high-ballast fuels, such as hard coal, DE 37 31 082 Cl a plant has been proposed, with at least one Boiler for burning the fuel, at least one steam turbine and a gas turbine for recovering energy from the flue gases of the boiler, a pollutant removal system having means for dedusting and desulfurizing the flue gases and a first gas-gas heat exchanger in which the dedusted and desulfurized clean gas is preheated by the crude gas coming from the boiler, wherein the clean gas brought into a heat-exchanging relationship with the raw gas is used in compressed form as engine gas for at least one downstream gas turbine.
  • a NO x - reduction system between the first gas-gas heat exchanger and a second gas-gas heat exchanger is involved.
  • the primary sides of these two gas-gas heat exchangers are connected in series and the further gas-gas heat exchanger is also supplied with the raw gases coming from the boiler.
  • At least for the clean gas inlet-side gas-gas heat exchanger is provided to control the outlet temperature of the pressurized clean gas with variable heat exchanger surfaces.
  • the reduction plant is designed as an SCR reactor and provided with a catalytically active adsorbent. It is thus to be achieved in processes with steam and gas turbines for effective and economical NO x emission reduction in all load ranges.
  • the flue gas leaving the boiler passes through the two gas-gas heat exchangers, is then dedusted, desulphurized and compressed, wherein the flue gas for heating the further flue gas heat exchanger passes before the catalytic reduction catalyst, ammonia is added as a reducing agent and thus fed to the reduction catalyst becomes.
  • the NO x largely liberated gas passes via a line to the secondary side of the gas-gas heat exchanger and is there from downstream of the boiler raw gas to the intended inlet temperature of about 900 0 C nachgesch'alteten one Gas turbine heated. Behind the gas turbine, the expanded flue gas is directed into an exhaust duct.
  • a preheating of the combustion air for the boiler can be done with the residual energy content of the purified flue gas.
  • From DE 36 29 817 C2 is a method for reducing the in the power generation of hard coal in power plants with combined gas / steam turbine processes with upstream coal pressure carburetor resulting pollutant emissions known.
  • the raw fuel gas is cleaned and burned the clean gas in the gas turbine combustion chamber with the addition of air.
  • the fuel gas is cooled in a heat exchanger to 200 0 C to 400 0 C for the subsequent dehalogenation and to condense the alkalis on the dust grains.
  • an absorption reactor operated with calcium carbonate chlorine and hydrogen fluoride are selectively chemically bound. Thereafter, the gas is dedusted, desulfurized and fed this pre-cleaned gas a gas turbine combustor.
  • the flue gas leaving this is cleaned with the addition of ammonia in a loaded with carbonaceous adsorbent as a catalyst further adsorption of NO x .
  • a waste heat boiler Prior to the introduction of the emerging from the gas turbine combustor flue gases in the denitrification a waste heat boiler is arranged in order to cool the flue gases to about 120 0 C for denitrification. In the waste heat boiler steam is generated from the remaining heat, from which in turn is obtained via a steam turbine set electrical energy.
  • the present invention has for its object to be able to operate a plant for cleaning the flue gases of a furnace more economical.
  • This object of the invention is achieved by the abovementioned system, in which an exhaust gas outlet of the at least one combustion device for generating electricity with a mixing chamber or a heat exchanger, which 'in the flue gas line to the reduction catalyst (8) are arranged' flow-connected, wherein a flue gas outlet of Mixing chamber or the heat exchanger with a flue gas inlet of the reduction catalyst is fluidly connected, or that the exhaust outlet of the at least one combustion device (19) for generating electricity directly to the flue gas inlet of the reduction catalyst (8) is fluidly connected, and optionally between the mixing chamber or the heat exchanger or the combustion device for Power generation and the reduction catalyst or in the reduction ⁇ catalyst, the supply means for the reducing agent ange- order, and by the method in which the flue gases for catalytic reduction are heated with at least one combustion device for generating electricity to a temperature in the range between 250 ° C and 500 ° C.
  • the advantage here is that those energy that is not converted into electricity, at least partially for the heating of the flue gas to a temperature of at least 250 0 C is used, whereby the particle size of the reduction catalyst for denitrification (SCR catalyst) can be reduced so that at least approximately the same surface of this reduction catalyst can be made more compact, since the reduction at higher temperatures has a better reaction kinetics.
  • the energy content of the fuel gas for the combustion device for power generation is thus better utilized, so that therefore the energy efficiency of this combustion device can be improved.
  • the inventive arrangement of the components of the flue gas cleaning system and the equipment cost is reduced.
  • this particulate matter separation can optionally be carried out in this reduction catalyst, wherein this particulate matter can subsequently be removed again, for example by periodic shaking or the like.
  • the flue gas can be heated by the combustion device for generating electricity to a temperature between 300 0 C and 400 0 C.
  • the mixing chamber or the heat exchanger can form a unit with the at least one combustion device (19) for power generation. It thus reduces the flow paths and consequently the heat losses and the system can be made more compact overall.
  • the at least one combustion device for generating electricity is a gas turbine or a gas engine, which is operated in particular with natural gas. It can thus be made available a large energy density in a compact design.
  • gas turbines or gas engines have a high operational reliability.
  • gas turbines or gas engines reach their full power within a short time, which makes them suitable for discontinuous operation, if desired. In particular, so that the required power is easily controlled.
  • low investment costs are required for gas turbines or gas engines.
  • the at least one combustion device for generating electricity may be arranged a mixing device for mixing the flue gases from the furnace with the clean gas for the combustion device for generating electricity.
  • a mixing device for mixing the flue gases from the furnace with the clean gas for the combustion device for generating electricity may be arranged.
  • a more intensive mixing of the flue gases with the fuel gas is possible, so that when the flue gases exit from this
  • Combustion means for generating electricity a more homogeneous temperature profile is present and thus an improvement of the reduction of nitrogen oxides and / or carbon monoxide and / or hydrocarbons in the reduction catalyst can be achieved.
  • it can also be achieved that, in the event that the flue gases still contain flammable components, their combustion in the incinerator for power generation can be better performed.
  • it can thus be introduced into the combustion device for generating electricity, a gas mixture which has a high degree of continuity in terms of its composition.
  • At least one heat exchanger may be arranged which is connected to an output of the at least one reduction catalytic converter, so that thus leaving the reduction catalytic converter, denitrified flue gases for preheating the flue gases from the Dust separation, which are fed to the denitrification, can be used and thus the energy yield of the flue gas cleaning process can be further increased.
  • At least one raw material drying plant or raw material grinding plant is arranged so that on the one hand the thermal energy contained in the flue gases can be better utilized and on the other hand the flue gases before entering the dust-collecting device are cooled down so far that the thermal load of the dust-collecting device can be reduced.
  • this is advantageous if a cloth filter or bag filter is used as dust removal device. It can be dispensed with additional cooling devices for this purpose.
  • the reducing agent is added to the flue gas originating from the furnace before the temperature increase in the at least one combustion device for generating electricity.
  • the reducing agent itself is heated to a higher temperature, whereby correspondingly positive effects in terms of the reaction in the reducing agent catalyst can be achieved
  • it can also be achieved that in the combustion device for power generation already a certain proportion of nitrogen oxides and / or carbon monoxide and / or hydrocarbons degraded by non-selective reduction, so that the nitrogen oxide content and / or the proportion of carbon monoxide and / or the proportion of hydrocarbons in the flue gas is lowered, and thus the required active catalyst surface can be reduced the reduction catalyst can be dimensioned smaller.
  • FIG. 1 shows a block diagram of an embodiment variant of a inventive system for flue gas cleaning as part of an overall system
  • Fig. 2 shows a detail of the overall system of another embodiment.
  • Fig. 1 shows a plant 1 for cement clinker production.
  • the denitrification plant according to the invention is not limited to use in the cement industry, although this is the preferred embodiment. It can also be equipped with waste incineration plants, caloric power plants, etc.
  • the plant 1 has a furnace 2 in the form of a rotary kiln, which is operated by a firing 3, whereby the cement clinker is formed from the known raw materials.
  • the flue gases leaving the furnace - arrow 4 - are introduced into a heat exchanger unit 5, which is designed in this embodiment in the form of a cyclone heat exchanger with four cyclones to use the energy content of the flue gases to preheat the raw meal used.
  • the heat exchanger unit 5 leaving the flue gas - arrow 6 - passes in the sequence in a gas purification plant.
  • This gas purification plant comprises at least one dust separation device 7 and at least one reduction device with a reduction catalyst 8.
  • the dust removal device 7 is designed as a bag filter. Bag filters are already known and used in the cement industry, so that further discussion is not necessary at this point. With the help of these filters, the Dust content of the flue gas reduced at least to values that meet the emission standards.
  • the flue gas which enters the bag filter or the dust removal device 7 may optionally be preconditioned with water.
  • a spraying device 10 can be arranged in a supply line 9, is sprayed with the water. It is thus also a cooling of the flue gas before entering the dust removal device 7 is reached, for example, a maximum of 250 0 C, whereby the thermal load of the dust collecting device 7 can be reduced by the flue gases.
  • the flue gas is diluted with fresh air via a fresh air line 11, in which a flap 12 is arranged, whereby the effectiveness of dedusting can be increased.
  • a mixed gas can be supplied to the flue gas via a mixed gas line 13, for example a gas originating from the furnace 2, a so-called bypass gas which can be withdrawn from the furnace 2 in the area of the heat exchanger unit 5.
  • the dust content of the flue gas or raw gas of about 50 g / Nm 3 to 150 g / Nm 3 to a value of less than 20 mg / Nm 3 , in particular at most 3 mg / Nm 3 , reduced.
  • the dust collecting device 7 may be provided with thermal insulation, so that the reduction of the flue gas temperature can be reduced.
  • the dust removal device 7 can also be replaced by other filters, for example cloth filters or coarse dedusting devices, such as electrostatic precipitators or the like. , which are all known from the prior art, be formed.
  • a gas-gas heat exchanger 15 may be provided to preheat the relatively cold flue gases from the dust-collecting device 7 for subsequent defrosting.
  • this heat exchanger 15 can be connected to an output 16 of the reduction catalytic converter 8 via an exhaust gas line 17.
  • heat exchanger 15 in particular a tube bundle heat exchanger is used.
  • other heat exchangers known in the art e.g. Plate heat exchangers, etc., can be used for this purpose.
  • the arrangement of the heat exchanger 15 for preheating the flue gases is a preferred embodiment, but is not mandatory. Accordingly, the flue gases from the dust separation device 7 can be introduced either directly or via the preheating with the heat exchanger 15 into a supply means 18 for a reducing agent, in particular ammonia or ammonia gas or at a higher temperature ammonia releasing reducing agent.
  • a reducing agent in particular ammonia or ammonia gas or at a higher temperature ammonia releasing reducing agent.
  • the reducing agent supply can be effected, for example, by means of spray nozzles, with preference being given to intimate mixing with the flue gas to be de-stiffened in the feed device 18.
  • the addition of reducing agent for so-called SCR denitrification plants from the prior art is known and should therefore be made at this point to the relevant literature.
  • combustion device 19 for power generation.
  • this combustion device 19 is formed for generating electricity by a so-called gas turbine, which is fired in particular with natural gas, wherein generally fossil fuels or even biomass can be used as fuel for the firing of the combustion device 19.
  • gas turbine which is fired in particular with natural gas
  • Other combustion devices 19 are also possible, such as, for example, diesel engines, etc.
  • the supply of the fuel gas to the combustion device 19 is indicated schematically in FIG.
  • the flue gases to be denitrified are heated to the working temperature of the reduction catalyst 8.
  • combustion means 19 for generating electricity to be denitrified flue gases to a temperature of at least 250 ° C and a maximum of 500 0 C are heated prior to their introduction into the reduction catalyst 8.
  • the flue gases to be denitrified be introduced directly into the combustion chamber of the combustion device 19 for power generation or it is alternatively possible that this combustion device 19 has a heat exchanger for generating electricity and the flue gases to be denitrated in this heat exchanger, either primary or on the secondary side, so that an indirect heating of the flue gases can be carried out.
  • a mixing chamber is arranged, in which the flue gases are mixed with the fuel gas.
  • the feed device 18 for feeding the reducing agent is not arranged in front of the combustion device 19, but instead If appropriate, it is also possible for the reduction catalytic converter 8 to comprise this supply device 18.
  • the reducing agent can be fed into or onto the catalyst bed.
  • the flue gas enters the reduction catalyst 8, wherein the denitrification, ie the implementation of the nitrogen oxides to nitrogen and water according to the known reactions, takes place.
  • the catalyst used can be, for example, titanium dioxide or vanadium pentoxide, optionally mixed with tungsten oxide or mixed with other metal oxides. In principle, these catalysts are known from the prior art, so that at this point a further discussion on its geometry or pore structure, etc. is unnecessary.
  • the formation of the catalyst bed per se is also state of the art, so that reference should be made to the relevant literature.
  • the reduction catalytic converter 8 it is possible for the reduction catalytic converter 8 to be arranged on a plurality of superimposed planes through which the flue gas flows in succession.
  • a conveyor device 14 can again be arranged between the vent 20 and the heat exchanger 15.
  • a heat recovery system 21 may be arranged, for example.
  • this heat recovery system 21 may be connected to a district heating network.
  • the residual energy content of the flue gases leaving the furnace 2 is preferably used for drying the raw materials used for the cement production.
  • two drying mills 22 are shown in Fig. 1, which are arranged in the flow direction of the flue gases between the furnace 2 and the dust collecting device 7.
  • these two drying mills 22 are connected in parallel, so that they can be flowed through simultaneously or alternatively by the flue gases to be de-nitrogenized.
  • Flaps 23-26 are shown in FIG. 1 for the corresponding circuit of the flow paths of the flue gas.
  • drying mills 22 can be connected in parallel to the direct introduction of the flue gases via a line 27 into the dust collecting device 7, for which purpose in this line 27, in turn, a flap 28 is arranged to order between the flow direction to be able to switch over the line 27 or at least one of the drying mills 22.
  • the drying mills 22 themselves are designed according to the state of the art.
  • a desulfurization plant is arranged, which may correspond to the prior art, to the sulfur content, ie to reduce the SO 2 content, at least partially in the flue gas.
  • Dust content of the flue gas leaving the furnace 2 or the heat exchanger 5 60 to 120 g / Nm 3
  • Dust content of the flue gas leaving the dust removal device 7 less than 20 mg / Nm 3
  • Temperature of the flue gases after the combustion device 19 for power generation 300 0 C to 340 0 C.
  • Temperature of the flue gases after the reduction catalyst 8 250 0 C to 320 0 C.
  • the dedusted flue gases from the combustion in the furnace 2 again enter the gas / gas heat exchanger 15 and are used here with the preheated exhaust gas leaving flue gases.
  • the flue gases with a maximum temperature of 150 0 C and a dust content of less than 20 mg / Nm 3 enter the heat exchanger 15 and are preheated to a temperature of about 220 0 C. This information is based on the normal operation of Appendix 1. When starting up this system 1, other values may result, since the flue gases may be even colder.
  • the thus preheated flue gases are supplied as a result of a gas / gas mixing chamber 33, in which they are mixed with the exhaust gas originating from the combustion device 19 for generating electricity.
  • the flue gases are heated to the operating temperature of the reduction catalyst 8, ie, for example, to a temperature of about 270 0 C, wherein the exhaust gas from the combustion device 19 for power generation may have a temperature of about 430 ° C.
  • the thus heated gas mixture is fed in the sequence in the reduction catalyst 8 for denitrification.
  • the entstickte flue gas is fed back to the heat exchanger 15 and finally leaves the system 1 via the vent 20, optionally after passing through the heat recovery device 21st
  • the flue gases can also be purified by carbon monoxide and, in particular, odoriferous hydrocarbons, or the plant 1 can also be used to remove ammonia from exhaust gases from incinerators.
  • a separate catalyst can be arranged before or after the denitrification catalyst, for example comprising titanium vanadium compounds which may be mixed with palladium and / or platinum.
  • the reduction catalyst 8 can be designed as a multilayer catalyst with multiple beds for the individual catalysts, or it is also possible to arrange several catalysts separately in the system 1 or a corresponding flue gas cleaning system, eg. in the flow direction of the flue gases one behind the other in their own containers.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Ceramic Engineering (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Organic Chemistry (AREA)
  • Structural Engineering (AREA)
  • Materials Engineering (AREA)
  • Thermal Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Biomedical Technology (AREA)
  • Physics & Mathematics (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Ecology (AREA)
  • Environmental Sciences (AREA)
  • Public Health (AREA)
  • Chimneys And Flues (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Abstract

L'invention se rapporte à une installation (1) destinée au nettoyage des fumées d'un four (2), comportant au moins un dispositif de dépoussiérage (7) agencé après le four (2) dans le sens d'écoulement des fumées, au moins un dispositif d'admission (18) placé après le ou les premiers dispositifs de dépoussiérage (7) et destiné à un agent réducteur pour assurer la réduction des oxydes d'azote et/ou du monoxyde de carbone et/ou notamment des hydrocarbures odoriférants contenus dans les fumées, et au moins avec un dispositif de combustion (19) pour produire de l'électricité. Une évacuation des gaz d'échappement du ou des dispositifs de combustion (19) pour produire de l'électricité est raccordée dans le sens d'écoulement à une chambre de mélange ou à un échangeur de chaleur respectivement agencés dans la conduite d'évacuation des fumées jusqu'au catalyseur de réduction (8), une évacuation de la chambre de mélange ou de l'échangeur de chaleur étant raccordée dans le sens d'écoulement à une admission des fumées du catalyseur de réduction (8) ou l'évacuation des gaz d'échappement du ou des dispositifs de combustion (19) pour produire de l'électricité étant directement reliée dans le sens d'écoulement à l'admission des fumées du catalyseur de réduction (8).
PCT/AT2009/000093 2008-03-06 2009-03-06 Installation de nettoyage des fumées d’un four Ceased WO2009108983A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ATA368/2008 2008-03-06
AT0036808A AT505542B1 (de) 2008-03-06 2008-03-06 Anlage zur reinigung der rauchgase eines ofens

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WO2009108983A1 true WO2009108983A1 (fr) 2009-09-11

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Cited By (3)

* Cited by examiner, † Cited by third party
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WO2016128545A1 (fr) * 2015-02-13 2016-08-18 Elex Cemcat Ag Procédé d'épuration de gaz d'échappement lors du retraitement thermique de matières minérales
CN112915731A (zh) * 2021-01-26 2021-06-08 天津理工大学 一种煅烧炉尾气净化处理装置及工艺
CN115055046A (zh) * 2022-06-15 2022-09-16 青岛格林特环保设备股份有限公司 一种用于环境污染治理的烟尘除硝除硫环保装置

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT507773B1 (de) 2009-07-15 2010-08-15 Scheuch Gmbh Verfahren und vorrichtung zur entstickung von rauchgasen
AT508921B1 (de) 2010-04-02 2011-05-15 Scheuch Gmbh Verfahren und vorrichtung zur entstickung von rauchgasen
DE102014100896A1 (de) * 2014-01-27 2015-07-30 Thyssenkrupp Ag Verfahren zur Wärmebehandlung eines Stoffstroms und zur Reinigung von dabei entstehenden Abgasen
DE102015208029A1 (de) * 2015-04-30 2016-11-03 Dürr Systems GmbH Reinigungsvorrichtung, Kalzinieranlage und Verfahren zum Reinigen eines Rohgasstroms

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU424421B2 (en) * 1968-10-31 1972-05-23 Gippsland Cement & Lime Co. Pty. Limited A process forthe production of cement clinker in vertical kilns
DE3629817A1 (de) * 1986-09-02 1988-03-03 Bergwerksverband Gmbh Verfahren zur verringerung der schadstoffemisionen von kraftwerken mit kombinierten gas-/dampfturbinenprozessen mit vorgeschalteter kohlevergasung
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