EP2237861A1 - Rauchgasreinigungsanlage - Google Patents
RauchgasreinigungsanlageInfo
- Publication number
- EP2237861A1 EP2237861A1 EP09702662A EP09702662A EP2237861A1 EP 2237861 A1 EP2237861 A1 EP 2237861A1 EP 09702662 A EP09702662 A EP 09702662A EP 09702662 A EP09702662 A EP 09702662A EP 2237861 A1 EP2237861 A1 EP 2237861A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- reduction
- catalyst
- flue gases
- filter device
- plant
- 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.)
- Withdrawn
Links
- 239000003546 flue gas Substances 0.000 title claims abstract description 83
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 238000000746 purification Methods 0.000 title description 3
- 239000003054 catalyst Substances 0.000 claims abstract description 54
- 239000000428 dust Substances 0.000 claims abstract description 45
- 230000009467 reduction Effects 0.000 claims abstract description 37
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 18
- 239000004568 cement Substances 0.000 claims abstract description 10
- 238000006722 reduction reaction Methods 0.000 claims description 36
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 22
- 238000001035 drying Methods 0.000 claims description 15
- 230000002829 reductive effect Effects 0.000 claims description 13
- 229910021529 ammonia Inorganic materials 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 11
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 10
- 239000012717 electrostatic precipitator Substances 0.000 claims description 10
- 238000000034 method Methods 0.000 claims description 10
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 6
- 238000004140 cleaning Methods 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 6
- 229930195733 hydrocarbon Natural products 0.000 claims description 5
- 150000002430 hydrocarbons Chemical class 0.000 claims description 5
- 238000006477 desulfuration reaction Methods 0.000 claims description 3
- 230000023556 desulfurization Effects 0.000 claims description 3
- 238000001556 precipitation Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 12
- 230000003197 catalytic effect Effects 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000004744 fabric Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000010304 firing Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- MGWGWNFMUOTEHG-UHFFFAOYSA-N 4-(3,5-dimethylphenyl)-1,3-thiazol-2-amine Chemical compound CC1=CC(C)=CC(C=2N=C(N)SC=2)=C1 MGWGWNFMUOTEHG-UHFFFAOYSA-N 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- -1 for example Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 235000012054 meals Nutrition 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005121 nitriding Methods 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- QGLKJKCYBOYXKC-UHFFFAOYSA-N nonaoxidotritungsten Chemical compound O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1 QGLKJKCYBOYXKC-UHFFFAOYSA-N 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000000523 sample Substances 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical class [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 description 1
- 229910001930 tungsten oxide Inorganic materials 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
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
- B01D53/8631—Processes characterised by a specific device
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
Definitions
- the invention relates to a system for purifying the flue gases of a furnace with at least one selective reduction catalyst for the reduction of nitrogen oxides contained in the flue gas and / or with at least one catalyst for the reduction of carbon monoxide, especially odoriferous, hydrocarbons or ammonia removal, and a Dust separation, and a method for purifying the flue gases of a furnace by selective catalytic reduction of nitrogen oxides with a reducing agent and a reduction catalyst and by dust deposition.
- 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 ° C and 1100 ° 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.
- Object of the present invention is to provide a system for denitrification of flue gases after the selective catalytic reduction process (SCR) and a method to provide which (s) in comparison to low-dust concepts a lower energy consumption and compared to high-dust plants has a longer service life of the catalyst.
- SCR selective catalytic reduction process
- This object of the invention is achieved by the aforementioned plant in which the dust is formed by at least a first and a second filter device and the reduction catalyst between the first and the second filter device is arranged, and by the method for cleaning the flue gases of a furnace in the The flue gases before they come into contact with the reduction catalyst are fed to a first dust separation and the fine dust cleaning of the flue gases takes place after the reduction of the nitrogen oxides.
- the circuit of the denitrification catalyst according to the invention has the advantage that the flue gases for the denitration reactions do not have to be additionally heated, but these flue gases still have a sufficient energy content, i. the sufficient temperature to be able to operate the catalyst. It can thus be achieved in comparison to low-dust plants, a reduction of fuels.
- the first filter device can be arranged in the flow direction of the flue gases immediately after the furnace or after a heat exchanger unit, so that the flue gases enter the first filter unit with a very high temperature, whereby the temperature drop in this filter unit - relatively speaking - can be kept low, and the flue gases leave the filter device at a temperature which favors the reduction of the nitrogen oxides on the catalyst.
- high temperature is meant a temperature of at least 250 ° C.
- the first filter device is an electrostatic precipitator.
- this filter can be operated at a high temperature, and on the other hand that this filter technology is already very mature or electrostatic precipitators, for example, are already present in plants for cement production - in the past the dedusting was often carried out with electric motors.
- electrostatic precipitators were largely replaced by cloth filters due to the stricter environmental requirements - and incur no additional investment costs.
- At least one raw material drying plant or raw material drying mill is arranged, so that the residual content of energy of the flue gases for drying of raw materials , which are used, for example, for cement production, can be used.
- this achieves the effect that the flue gases leaving the catalyst bed are cooled even further before being subjected to the second filter device, which is preferably formed by a cloth filter, as a result of which this second filter device is subject to a lower thermal load even without the use of additional cooling devices.
- the dust content of the flue gases in the first dust separation to a dust content of max. 3 g / Nm 3 , in particular max. 2.5 g / Nm 3 , for example, max. 1 g / Nm 3 , or of max. 30 g / Nm 3 , if another pre-separator, so no electrostatic precipitator, is used as the first filter device, reduced because it has been found that the efficiency of the system can be increased at these maximum dust levels of the flue gases.
- the first dust separation is carried out at a temperature of the flue gas which is at least 250 ° C or at most 450 ° C, for example at most 350 ° C, whereby, as stated above, to special measures to reduce the temperature drop in The first filter device can be dispensed with and this can thus be made cheaper.
- FIG. 1 A plant according to the invention in the form of a block diagram.
- 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 formed in this embodiment in the form of a cyclone heat exchanger with in 4 cyclones to use the energy content of the flue gases to preheat the raw meal used.
- the heat exchanger unit 5 leaving flue gas - arrow 6 - occurs in the sequence in the gas purification system.
- This gas purification system comprises a first filter device 7, a reduction catalytic converter 8 and a second filter device 9.
- the first filter device 7 is designed as an electrostatic precipitator.
- the flue gas entering the electrostatic precipitator may optionally be preconditioned with water to increase the effectiveness of the electrostatic precipitator.
- a spraying device 11 can be arranged in a supply line 10 to the first filter device 7, is sprayed with the water.
- a mixed gas can be supplied to the flue gas via a mixed gas line 14, for example a gas originating from the furnace 2, a so-called bypass gas which can be withdrawn from the furnace 2 in the region of the heat exchanger unit 5.
- Both in the mixed gas line 14 and in the supply line 10 corresponding conveying devices 15, such as exhaust fan, may be arranged.
- the first filter device 7 may be provided with a thermal insulation which is suitable for these high temperatures, so that the reduction in the Raugastemperatur can be reduced.
- the flue gas enters the reduction catalyst 8, wherein the end nitriding, ie the implementation of the nitrogen oxides to nitrogen and water according to the known reactions takes place.
- a reducing agent is supplied by means of a reducing agent feed 16.
- a reducing agent is usually ammonia used, as is known from the prior art. However, it is also possible to use ammonia-containing compounds or reducing agents which release ammonia at the elevated temperature.
- the reducing agent feed 16 can also be dispensed with if excess ammonia is present in the exhaust gas of the plant 1 or, if the ammonia is too low, only the missing fraction can be supplied via the reducing agent feed 16.
- titanium dioxide or vanadium pentoxide or titanium oxide as a carrier with vanadium pentoxide as the active composition, optionally mixed with tungsten oxide or mixed with other metal oxides.
- 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 supply of reducing agent takes place, for example, again via spray nozzles.
- the reducing agent itself can be added to the flue gas before the catalyst, but this reducing agent is preferably fed into or onto the catalyst bed.
- 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 it is possible for the reduction catalytic converter to be arranged on a plurality of superimposed planes through which the flue gas flows in succession.
- the de-stoked flue gas - it should be mentioned at this point that with denestered flue gas a flue gas is meant, which corresponds to NO x the emission standards, eg the Austrian emission standards - passes via a line 17 to the second filter device 9.
- This second filter device 9 is a bag filter executed, with filter cloths or filter bags. Also these bag filters are already known and used in the cement industry, so that further discussion is not necessary at this point. With the aid of these filter cloths, the dust content of the flue gas is at least reduced to values which correspond to the exhaust gas standards.
- a spray cooling 18 may be arranged in front of the second filter device 9 to cool the flue gas before entering the second filter device 9 to a temperature, for example a maximum of 250 ° C, which reduces the thermal load of the filter cloth by the flue gases.
- a conveying device 15 can again be arranged between the vent 19 and the second filter device 9.
- the residual energy content of the flue gases leaving the reduction catalytic converter 8 is preferably used for drying the raw materials used for cement production.
- two drying mills 20 are shown in Fig. 1, which are arranged in the flow direction of the flue gases between the reduction catalyst 8 and the second filter device 9.
- these two drying mills 20 are connected in parallel, so that they can be flowed through simultaneously or alternatively by the denitrified flue gases.
- For the corresponding circuit of the flow paths of the flue gas flaps 21 - 24 are shown in Fig. 1.
- drying mills 20 can be connected in parallel to the direct introduction of the flue gases via the line 17 in the second filter device 9, including in this line 17, in turn, a flap 25 is arranged to order between the Flow direction can be switched over the line 17 or at least one of the drying mills 20.
- the drying mills 20 themselves are designed according to the state of the art.
- 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 electrostatic precipitator max. 3 g / Nm 3
- Temperature of the flue gases after the reduction catalyst 8 280 ° C to 320 ° C.
- Dust content of the flue gas entering the bag filter less than 3 g / Nm 3 for direct discharge or approx. 100 g / Nm 3 for "mill operation"
- Dust content of the flue gas when leaving the bag filter max. 10 mg / Nm 3
- the dust content of the flue gases in the reduction catalyst 8 is practically not reduced. If, nevertheless, a dust precipitation takes place in the reduction catalytic converter 8, this can be cleaned periodically, for example by blowing with compressed air.
- the flue gas and carbon monoxide from, in particular, odoriferous, hydrocarbons or ammonia removal from exhaust gases from incinerators, especially the Appendix 1, are used.
- a separate catalyst can be arranged before or after the denitrification catalyst, for example comprising titanium vanadium compounds which can be mixed with palladium and / or platinum.
- Such catalysts are known from the prior art, so reference should be made to the relevant literature.
- the reduction catalyst 8 can be designed as a multilayer catalyst with multiple beds for the individual catalysts, or there is also the possibility of several catalysts separately in the system 1 or a corresponding flue gas cleaning system are arranged, for example, in the flow direction of the flue gases behind each other in their own containers.
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Treating Waste Gases (AREA)
- Electrostatic Separation (AREA)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AT0003108U AT10369U1 (de) | 2008-01-16 | 2008-01-16 | Rauchgasreinigungsanlage |
| PCT/AT2009/000010 WO2009089559A1 (de) | 2008-01-16 | 2009-01-15 | Rauchgasreinigungsanlage |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| EP2237861A1 true EP2237861A1 (de) | 2010-10-13 |
Family
ID=40104815
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP09702662A Withdrawn EP2237861A1 (de) | 2008-01-16 | 2009-01-15 | Rauchgasreinigungsanlage |
Country Status (7)
| Country | Link |
|---|---|
| US (1) | US20100307388A1 (zh) |
| EP (1) | EP2237861A1 (zh) |
| CN (1) | CN101977668A (zh) |
| AT (1) | AT10369U1 (zh) |
| BR (1) | BRPI0907170A2 (zh) |
| RU (1) | RU2484883C2 (zh) |
| WO (1) | WO2009089559A1 (zh) |
Families Citing this family (26)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009118336A1 (fr) * | 2008-03-25 | 2009-10-01 | Agc Flat Glass Europe Sa | Four de fusion du verre |
| DE102009022903A1 (de) * | 2009-05-27 | 2010-12-09 | Polysius Ag | Verfahren und Anlage zur Wärmebehandlung von feinkörnigem Material |
| DE102010036647B3 (de) | 2010-07-27 | 2012-01-19 | Elex Cemcat Ag | Rauchgasreinigungsanlage einer Zementklinkerproduktionsanlage |
| DE102011000564B4 (de) | 2011-02-08 | 2013-05-02 | Elex Cemcat Ag | Verfahren und Anlage zur Herstellung von Zementklinker |
| DE102011001773B4 (de) * | 2011-04-04 | 2013-01-24 | Thyssenkrupp Polysius Ag | Verfahren und Anlage zur Herstellung von Zementklinker |
| AT510406B1 (de) * | 2011-04-04 | 2012-04-15 | Scheuch Gmbh | Schlauchfilter zur reinigung staubbelasteter gase und injektordüse für ein solches schlauchfilter |
| DE102011001933B4 (de) | 2011-04-08 | 2013-02-28 | Elex Cemcat Ag | Verfahren und Anlage zur Herstellung von Zementklinker und zur Reinigung der dabei entstehenden Abgase |
| DE102011050125B4 (de) * | 2011-05-05 | 2019-04-18 | Maerz Ofenbau Ag | Rauchgasreinigungsanlage einer Zementklinkerproduktionsanlage |
| DE102011050677B4 (de) * | 2011-05-27 | 2014-08-28 | Südbayerisches Portland-Zementwerk Gebr. Wiesböck & Co. GmbH | Vorrichtung und Verfahren zur Herstellung von Zementklinker |
| US20140170046A1 (en) * | 2011-07-29 | 2014-06-19 | Flsmidth A/S | Pollution control system for kiln exhaust |
| CN102935331A (zh) * | 2011-08-15 | 2013-02-20 | 上海索菲玛汽车滤清器有限公司 | 用于还原废气中的氮氧化物的设备 |
| CN102661667A (zh) * | 2012-05-31 | 2012-09-12 | 河南中材环保有限公司 | 一种水泥窑炉脱硝、余热利用及除尘系统及方法 |
| DE102013016701B4 (de) * | 2013-10-08 | 2017-06-14 | Khd Humboldt Wedag Gmbh | Verfahren zur Entstickung von Bypassabgasen in einer Anlage zur Herstellung von Zementklinker und Anlage zur Herstellung von Zementklinker |
| DE102013112210A1 (de) * | 2013-11-06 | 2015-05-07 | Thyssenkrupp Ag | Verfahren zur Reinigung von Bypassgasen der Zement- oder Mineralsindustrie sowie Anlage der Zement- oder Mineralsindustrie |
| DE102014100896A1 (de) * | 2014-01-27 | 2015-07-30 | Thyssenkrupp Ag | Verfahren zur Wärmebehandlung eines Stoffstroms und zur Reinigung von dabei entstehenden Abgasen |
| EP3002051B1 (en) * | 2014-10-03 | 2019-12-25 | General Electric Technology GmbH | Dust separator useful with dry scrubber system |
| DE102015202698B4 (de) | 2015-02-13 | 2020-11-05 | Maerz Ofenbau Ag | Verfahren zur Reinigung von Abgasen bei der thermischen Aufarbeitung von Mineralstoffen |
| CN107781834A (zh) * | 2016-08-30 | 2018-03-09 | 中国辐射防护研究院 | 一种废浸渍活性炭焚烧处理装置及方法 |
| DE102016119695A1 (de) * | 2016-10-17 | 2018-04-19 | Thyssenkrupp Ag | Verfahren und Anlage zur Reinigung von Vorwärmerabgasen einer Anlage der Zement- und/oder Mineralsindustrie |
| CN108426263B (zh) * | 2018-03-28 | 2019-10-18 | 清华大学 | 燃煤烟气处理系统 |
| DE212020000396U1 (de) * | 2020-12-21 | 2021-02-17 | Suzhou Xiquan Software Technology Co., Ltd | Behandlungsvorrichtung für Abgase des Kessels zum Bedrucken und Färben |
| AT17408U1 (de) * | 2021-03-24 | 2022-03-15 | Scheuch Man Holding Gmbh | Vorrichtung und Verfahren zur Herstellung von Zementklinker |
| CN113069920A (zh) * | 2021-05-08 | 2021-07-06 | 中材萍乡水泥有限公司 | 一种水泥生产超低排放脱硝设备 |
| CN114471108B (zh) * | 2022-02-14 | 2022-12-27 | 北京科技大学 | 工业烟气同步脱碳脱硝及余热回收利用的装置 |
| CN114870620A (zh) * | 2022-05-07 | 2022-08-09 | 北京京西燃气热电有限公司 | 一种柔性接触式密封装置 |
| CN116747643B (zh) * | 2023-08-24 | 2023-12-19 | 山西毅诚科信科技有限公司 | 一种新型水泥窑脱硝除尘装置 |
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| DE3642179A1 (de) * | 1986-12-10 | 1988-06-23 | Hoelter Heinz | Verfahren und vorrichtung zur simultanen so(pfeil abwaerts)2(pfeil abwaerts)- und no(pfeil abwaerts)x(pfeil abwaerts)-abscheidung hinter feuerungsanlagen mit koks-precoat-filter-system |
| SU1749633A1 (ru) * | 1990-03-01 | 1992-07-23 | А.И Жигайлов | Устройство дл очистки газов от цементной пыли и других примесей |
| RU2001672C1 (ru) * | 1990-11-26 | 1993-10-30 | Александр Маркович Гольдман | Установка дл очистки дымовых газов от сернистого ангидрида и окислов азота |
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| DE19612240A1 (de) | 1996-03-27 | 1997-10-02 | Abb Patent Gmbh | Verfahren und Vorrichtung zur Abscheidung von Schadstoffen, insbesondere von Stickoxiden, aus Rauchgas |
| DE19635383A1 (de) | 1996-08-31 | 1998-03-05 | Katalysatorenwerke Huels Gmbh | DeNOx-Katalysator für stark Staub-haltige Abgase |
| US6395237B1 (en) * | 2000-02-13 | 2002-05-28 | The Babcock & Wilcox Company | Circulating fluidized bed reactor with selective catalytic reduction |
| FR2817487B1 (fr) * | 2000-12-04 | 2003-02-21 | Lab Sa | Procede et installation d'epuration de fumees de cimenterie |
| US7198698B1 (en) * | 2001-05-02 | 2007-04-03 | Air Control Techniques, P.C. | Method of photochemically removing ammonia from gas streams |
| DE10227639B4 (de) * | 2002-06-20 | 2006-06-22 | Steag Encotec Gmbh | Kohlekraftwerk |
| FR2856938B1 (fr) * | 2003-07-01 | 2005-09-02 | Lab Sa | Procede et installation d'epuration de fumees, associant deux unites de separation et une epuration catalytique |
| JP2005028210A (ja) * | 2003-07-07 | 2005-02-03 | Mitsubishi Heavy Ind Ltd | 排ガス処理システム |
-
2008
- 2008-01-16 AT AT0003108U patent/AT10369U1/de not_active IP Right Cessation
-
2009
- 2009-01-15 EP EP09702662A patent/EP2237861A1/de not_active Withdrawn
- 2009-01-15 US US12/863,248 patent/US20100307388A1/en not_active Abandoned
- 2009-01-15 BR BRPI0907170A patent/BRPI0907170A2/pt not_active IP Right Cessation
- 2009-01-15 RU RU2010134000/05A patent/RU2484883C2/ru not_active IP Right Cessation
- 2009-01-15 CN CN2009801092597A patent/CN101977668A/zh active Pending
- 2009-01-15 WO PCT/AT2009/000010 patent/WO2009089559A1/de active Application Filing
Non-Patent Citations (1)
| Title |
|---|
| See references of WO2009089559A1 * |
Also Published As
| Publication number | Publication date |
|---|---|
| BRPI0907170A2 (pt) | 2017-06-06 |
| CN101977668A (zh) | 2011-02-16 |
| US20100307388A1 (en) | 2010-12-09 |
| AT10369U1 (de) | 2009-02-15 |
| RU2010134000A (ru) | 2012-02-27 |
| RU2484883C2 (ru) | 2013-06-20 |
| WO2009089559A1 (de) | 2009-07-23 |
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