WO2005005025A1 - 燃焼排ガス処理装置及び処理方法 - Google Patents
燃焼排ガス処理装置及び処理方法 Download PDFInfo
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- WO2005005025A1 WO2005005025A1 PCT/JP2004/009097 JP2004009097W WO2005005025A1 WO 2005005025 A1 WO2005005025 A1 WO 2005005025A1 JP 2004009097 W JP2004009097 W JP 2004009097W WO 2005005025 A1 WO2005005025 A1 WO 2005005025A1
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- WIPO (PCT)
- Prior art keywords
- exhaust gas
- combustion exhaust
- dust collector
- flue gas
- wet
- Prior art date
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Classifications
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- 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
-
- 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
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/64—Heavy metals or compounds thereof, e.g. mercury
-
- 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
-
- 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
- B01D53/8659—Removing halogens or halogen compounds
- B01D53/8662—Organic halogen compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/104—Ozone
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/108—Halogens or halogen compounds
Definitions
- the present invention relates to a flue gas treatment apparatus and treatment method, and more particularly to a flue gas for removing harmful substances such as dust, N ⁇ x, and dioxins in flue gas from a combustion furnace such as a cement kiln.
- the present invention relates to an exhaust gas treatment device and a treatment method.
- Patent Document 1 discloses that exhaust gas from an incinerator is passed through a first heat exchanger in order to remove dust, S ⁇ x, N ⁇ x, dioxins and the like contained in the exhaust gas from the incinerator. After collecting heat, the dust is collected by a cyclone and an electrostatic precipitator, SOx and NOx are removed by a scrubber, and the exhaust gas is heated to 100-200 ° C by a second heat exchanger.
- a technique is disclosed in which activated carbon powder is added to adsorb harmful components, and the activated carbon powder filtered through a bag filter is recovered.
- Patent Document 2 describes removal of harmful substances such as dust, dioxins, PCBs and other halogenated organic compounds from exhaust gas from an exhaust gas source such as a refuse incinerator. Even if the concentration of dust in the exhaust gas is high using an adsorbent such as activated carbon, the dust is removed efficiently, even if the dust concentration in the exhaust gas is high.
- An exhaust gas treatment device is disclosed.
- Patent Documents 3 and 4 disclose oxidation and decomposition treatment of dioxins in exhaust gas discharged from an exhaust gas source such as an incinerator. Therefore, there is disclosed an exhaust gas treatment apparatus in which ozone is contained in water and ozone-containing water is sprayed in a granular form into exhaust gas flowing through the temperature reducing cylinder by a nozzle disposed in the temperature reducing cylinder.
- Patent Document 5 discloses that in order to remove N ⁇ x and dioxins in exhaust gas generated by a municipal solid waste incinerator or the like, the exhaust gas is cooled, and the cooled exhaust gas is introduced into a bag filter.
- the cement firing equipment 21 includes a preheater 22, a calciner 23, a cement quinolene 24, a clean power cooler 25, etc., and the cement raw material supplied to the preheater 22 from the raw material supply system.
- R is preheated in the preheater 22, calcined in the calciner 23, and calcined in the cement kiln 24, and the produced clean power C 1 is cooled in the clean power cooler 25.
- the treatment of the combustion exhaust gas from the cement kiln 24 since limestone as a main raw material has a property of adsorbing S ⁇ x, desulfurization in the preheater 22 and dust collection by the electric precipitator 26 are performed. The flue gas was released to the atmosphere via fan 27 and chimney 28.
- Patent Document 1 JP 2001-272023 A
- Patent Document 2 Japanese Patent Application Laid-Open No. 2003-117343
- Patent Document 3 JP-A-2000-185217
- Patent Document 4 JP 2003-24746
- Patent Document 5 JP-A-7-75720
- cement firing equipment 21 shown in FIG. ability to input various types of recycled resources into raw materials If the input of recycled resources continues to increase in the future, there is a concern that the same harmful substance emissions and operating costs as in the above-mentioned municipal solid waste incinerators will increase. . In particular, since the combustion exhaust gas generated by the cement sintering facility 1 is large, even if the amount of harmful substances contained is very small, the equipment for removing harmful substances becomes large-scale, and equipment and operation costs are reduced. May lead to an increase.
- the present invention has been made in view of the above-mentioned problems in the conventional technology, and
- the present invention provides a dust collector for collecting dust in flue gas, a wet dust collector for collecting water-soluble components and dust in flue gas that has passed through the dust collector, and a wet type dust collector.
- a catalyst tower for decomposing and removing N ⁇ x and / or dioxins in the combustion exhaust gas that has passed through the dust collector.
- the water-soluble components and dust of the flue gas that has passed through the dust collector are collected by the wet dust collector, and the dust, sulfuric acid mist, and hydrogen chloride that greatly affect the life of the subsequent catalyst tower are collected.
- HC1, mercury (Hg), etc. can be removed, and then N ⁇ x and dioxins can be decomposed in the catalyst tower.
- denitration agents is reduced compared to non-catalytic denitration, and the use of adsorbents that require secondary treatment can be minimized in decomposing NOx and dioxins.
- unnecessary dust can be reused without becoming wet ash.
- a reheater for heating the flue gas discharged from the wet dust collector may be provided at a stage preceding the catalyst tower.
- the temperature of the combustion exhaust gas at the inlet of the catalyst tower can be raised to 170 ° C. or more, and denitration and decomposition of dioxins can be performed more effectively in the catalyst tower.
- an oxidant addition device that adds an oxidant to the combustion exhaust gas that has passed through the dust collector may be provided.
- an oxidant addition device that adds an oxidant to the combustion exhaust gas that has passed through the dust collector.
- acid Sodium hypochlorite and / or ozone can be used as the agent.
- ozone the decomposition rate increases in an alkaline atmosphere, so it is necessary to add a chemical to keep the pH of the circulating water acidic at about 5 or less.
- a solid-liquid separator for solid-liquid separating the slurry discharged from the wet dust collector, and a mercury adsorption tower for adsorbing mercury in the liquid separated by the solid-liquid separator are provided.
- a heat recovery device may be provided at a subsequent stage of the catalyst tower to use the flue gas discharged from the catalyst tower and raise the temperature of the gas supplied from the reheater. can do. As a result, the amount of auxiliary steam supplied to the reheater can be reduced, and the operating cost can be reduced.
- a mixing scrubber can be used for the wet dust collector.
- a high-efficiency scrubber such as a mixing scrubber, it is possible to efficiently remove dust, sulfuric acid mist, hydrogen chloride (HC1), mercury (Hg), etc., which greatly affect the life of the subsequent catalyst tower. it can.
- the flue gas may be a cement kiln flue gas.
- the present invention also relates to a method for treating flue gas, comprising collecting dust in the flue gas, wet-collecting water-soluble components and dust in the flue gas after the dust collection, and collecting the water-soluble component. It decomposes and removes N ⁇ x and Z or dioxins in exhaust gas using a catalyst.
- inexpensive equipment can be used to reduce the use of denitration agents and minimize the use of adsorbents and other substances that require secondary treatment when decomposing N ⁇ x and dioxins. Can be held down.
- the combustion exhaust gas can be heated before N ⁇ x and / or dioxins in the combustion exhaust gas are decomposed and removed using a catalyst. This makes it possible to more effectively denitrate and decompose dioxins in the catalyst tower.
- An oxidizing agent is added to the flue gas after dust collection to oxidize mercury and the like, and then the flue gas can be absorbed in a subsequent wet dust collector.
- the oxidizing agent sodium hypochlorite and / or ozone or the like can be used.
- the slurry generated by the wet collection may be subjected to solid-liquid separation, and mercury in the separated liquid may be adsorbed and removed. Further, by setting the residence time of the exhaust gas in the wet type dust collector to be 1 second or more and 10 seconds or less, it is possible to prevent the apparatus from becoming too large. Further, a cement kiln exhaust gas can be treated as the combustion exhaust gas.
- FIG. 1 shows an embodiment of a combustion exhaust gas treatment apparatus and a treatment method according to the present invention.
- the combustion exhaust gas treatment apparatus and the treatment method according to the present invention An example in which the present invention is applied to the treatment of flue gas from a kiln will be described.
- the cement sintering facility 1 includes a preheater 2, a calciner 3, a cement kiln 4, a cleansing cooler 5, and the like. Is supplied to the preheater 2, and is subjected to preheating in the preheater 2, calcination in the calcination furnace 3, and calcination in the cement kiln 4, thereby producing a cement cleaner C 1. This cement clinker C1 is cooled in the clinker cooler 5 and then pulverized in the finishing step.
- the flue gas treatment apparatus includes an electric dust collector 6 disposed downstream of the cement sintering facility 1, a wet dust collector 7 for collecting water-soluble components and dust in the flue gas, a reheater 11, Catalyst tower 12 for decomposing and removing NOx, etc., heat recovery unit 13, solid-liquid separator 16 for solid-liquid separation of slurry discharged from wet dust collector 7, and liquid separated by solid-liquid separator 16 It consists of a mercury adsorption tower 17 that adsorbs mercury inside.
- the electric dust collector 6 is provided for collecting dust in the combustion exhaust gas G from the preheater 2. Note that a bag filter can be used instead of the electric dust collector 6, and both are installed together. Talk about things.
- the wet dust collector 7 is provided for collecting water-soluble components and dust in the combustion exhaust gas G, and greatly affects the service life of the downstream catalyst tower 12, such as dust, sulfuric acid mist, and hydrogen chloride (HC1). ), Mercury (Hg), etc. can be removed.
- a mixing scrubber such as a mouse scrubber manufactured by Mu Company Limited
- the mixing scrubber is defined as having a plurality of guide vanes arranged in a cylindrical body, in which gas and liquid move in a countercurrent or a parallel flow in the cylindrical body, and in the process of turning the flow. It is a device that brings gas and liquid into contact with each other, and performs reactions and dust collection.
- the gas and the liquid are made to flow in parallel, and guide vanes that give a right turn to the flow and guide vanes that give a left turn are alternately arranged.
- the residence time of the combustion exhaust gas of the wet dust collector 7 is set to 1 second to 10 seconds.
- a circulation tank 7a is disposed below the wet dust collector 7, and a pump 9 is provided between the wet dust collector 7 and the circulation tank 7a.
- the slurry generated in the wet dust collector 7 is passed through the circulation tank 7a and the pump 9 The ability to circulate by S.
- the oxidizing agent adding device 10 is provided for adding sodium hypochlorite, ozone and the like as oxidizing agents for oxidizing mercury and the like contained in the combustion exhaust gas G.
- the reheater 11 is provided for heating the combustion exhaust gas G discharged from the mist separator 8.
- the purpose of heating the flue gas G is to denitrate and decompose dioxins more effectively in the catalyst tower.
- Ammonia (NH 3) used as a reducing agent in the subsequent catalyst tower 12 is added to the inlet side of the reheater 11.
- the reason for the addition in the preceding stage of (2) is to utilize the mixing effect of the fan and the reheater 11, and the mixing is performed between the outlet of the wet dust collector 7 and the inlet of the catalyst tower 12 except for the inlet side of the reheater 11. It can be added to places where the synergistic effect can be utilized.
- the catalyst tower 12 is provided to decompose and remove NOx and dioxins in the combustion exhaust gas G that has passed through the electrostatic precipitator 6.
- the catalyst tower 7 is configured in a honeycomb shape, and can be configured to be relatively small even when processing a large amount of combustion exhaust gas.
- the heat recovery unit 13 performs heat exchange between the combustion exhaust gas G discharged from the catalyst tower 12 and the gas from the reheater 11, and heat recovered from the combustion exhaust gas G is re-heated by the reheater 11. Use.
- a heat pipe is used in place of the heat recovery unit 13 and the reheater 11, and the heat exhausted from the catalyst tower 12 in the evaporation section of the pipe. It is also possible to adopt a configuration in which the heat from the combustion exhaust gas G is absorbed and the heat is dissipated in the condensing section of the pipe provided on the inlet side of the catalyst tower 12.
- a Jungstrom (registered trademark) type heat exchanger manufactured by Alstom Co., Ltd.
- the solid-liquid separator 16 separates the slurry discharged from the wet dust collector 7 into a solid and a liquid, and may use a micro filter or the like.
- the mercury adsorption tower 17 is provided to adsorb mercury in the liquid separated by the solid-liquid separator 16, and the wastewater treatment equipment 18 processes the liquid after adsorbing the mercury and converts the liquid into a river or the like. Release to. It is considered that, for example, oxidative decomposition treatment with ozone is suitable for the water treatment here. A part of the wastewater after passing through the mercury adsorption tower 17 can be reused in the wet dust collector 7. Further, waste water from the wet dust collector 7 can be used for cooling the combustion exhaust gas W of the cement kiln 4 and the like.
- the flue gas G from the cement kiln 4 desulfurized in the preheater 2 is brought to the electric precipitator 6, and the dust in the flue gas G is recovered.
- the combustion exhaust gas G that has passed through the electric dust collector 6 is introduced into the wet dust collector 7, where water-soluble components and dust in the combustion exhaust gas G are collected, and the dust, which greatly affects the life of the subsequent catalyst tower, is removed. Remove sulfuric acid mist, hydrogen chloride (HC1), mercury (Hg), etc.
- the slurry generated by the wet dust collector 7 is circulated through the circulation tank 7a and the pump 9, so that the exhaust gas W and the liquid are sufficiently brought into contact with each other, and Oxidation of mercury and the like with sodium chlorate and the like, and recovery of water-soluble components and dust can be performed efficiently.
- water is circulated and a part of the water is extracted and supplied to the solid-liquid separator 16.
- the circulating water is drained to such an extent that re-evaporation of the water-soluble components does not pose a problem.
- the combustion exhaust gas G from which water-soluble components, dust, etc. have been removed is re-added from the mist separator 8. It is introduced into the heater 11 and heated.
- the reason why the flue gas G is heated is that the denitration of the flue gas G and the decomposition of dioxins in the catalyst tower 12 are preferably carried out at 170 to 500 ° C, and considering the decomposition performance and durability of the catalyst, 230 — Decomposition at about 270 ° C is preferred.
- the wet dust collector 7 removes dust, sulfuric acid mist, hydrogen chloride (HC1), mercury (Hg), etc., which greatly affect the life of the subsequent catalyst tower 12, as shown in FIG.
- a mixing scrubber in this test example, a mouse scrubber manufactured by Mu Company Limited, Inc.
- the life of the catalyst in the catalyst tower 12 is maintained longer than in the case of a conventional horizontal scrubber.
- the combustion gas G discharged from the catalyst tower 12 is used as the heat source of the reheater 11.
- the combustion gas G discharged from the catalyst tower 12 is subjected to heat exchange with the gas introduced from the reheater 11 in the heat recovery unit 13, and the recovered heat is used in the reheater 11. Since the heat recovered by the heat recovery unit 13 alone cannot cover the amount of heat consumed by the reheater 11, the auxiliary steam S is introduced into the reheater 11. Further, ammonia (NH 3) as a denitration agent used in the catalyst tower 12 is injected into the inlet side of the reheater 11. As described above, ammonia is supplied to the reheater 1
- the combustion exhaust gas G is supplied to the catalyst tower 12, and NOx and dioxins are decomposed.
- the temperature in the catalyst tower 12 is controlled to 170 ° C. to 500 ° C., preferably 230 to 270 ° C., which is suitable for denitration of the flue gas G and decomposition of dioxins.
- the heat recovery unit 13 is disposed at the subsequent stage of the catalyst tower 12, it is possible to control the temperature inside the catalyst tower 12 high, and by increasing the operating temperature of the catalyst tower 12 as much as possible, The efficiency of the tower 12 increases, and the amount of catalyst used can be reduced.
- the combustion exhaust gas G from the catalyst tower 12 is discharged to the atmosphere via the heat recovery unit 13, the fan 14, and the chimney 15.
- the temperature of the flue gas G at the outlet of the fan 14 is controlled to about 110 ° C.
- the slurry discharged from the circulation tank 7a is subjected to solid-liquid separation by a solid-liquid separator 16 and
- the mercury in the separated liquid is dissolved in water as chromate complex ion (HgC14), which is absorbed in the mercury adsorption tower 17 and treated outside the system.
- the liquid from which mercury has been removed is treated as wastewater treatment equipment It is treated at 18 and can be reused by the wet dust collector 7 or used to cool the flue gas G of the cement kiln 4.
- FIG. 1 is a flowchart showing one embodiment of a combustion exhaust gas treatment apparatus according to the present invention.
- FIG. 2 is a graph showing the relationship between the type of wet dust collector of the flue gas treatment apparatus according to the present invention and the denitration rate in the denitration tower.
- FIG. 3 is a flowchart showing an example of a conventional cement burning facility.
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DK04746566.1T DK1649922T3 (da) | 2003-07-10 | 2004-06-28 | Indretning og fremgangsmåde til behandling af forbrændt udstødningsgas |
DE602004031231T DE602004031231D1 (de) | 2003-07-10 | 2004-06-28 | Vorrichtung und verfahren zur behandlung von verbrennungsabgas |
US10/561,479 US7799297B2 (en) | 2003-07-10 | 2004-06-28 | Device and method for processing combustion exhaust gas |
EP04746566A EP1649922B1 (en) | 2003-07-10 | 2004-06-28 | Device and method for processing combustion exhaust gas |
JP2005511495A JP4615443B2 (ja) | 2003-07-10 | 2004-06-28 | 燃焼排ガス処理装置及び処理方法 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2003-272896 | 2003-07-10 | ||
JP2003272896 | 2003-07-10 |
Publications (2)
Publication Number | Publication Date |
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WO2005005025A1 true WO2005005025A1 (ja) | 2005-01-20 |
WO2005005025B1 WO2005005025B1 (ja) | 2005-03-17 |
Family
ID=34055993
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/JP2004/009097 WO2005005025A1 (ja) | 2003-07-10 | 2004-06-28 | 燃焼排ガス処理装置及び処理方法 |
Country Status (10)
Country | Link |
---|---|
US (1) | US7799297B2 (ja) |
EP (1) | EP1649922B1 (ja) |
JP (2) | JP4615443B2 (ja) |
KR (1) | KR20060029135A (ja) |
CN (1) | CN1812828A (ja) |
DE (1) | DE602004031231D1 (ja) |
DK (1) | DK1649922T3 (ja) |
ES (1) | ES2357647T3 (ja) |
TW (1) | TWI336269B (ja) |
WO (1) | WO2005005025A1 (ja) |
Cited By (12)
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JP2006239492A (ja) * | 2005-03-01 | 2006-09-14 | Taiheiyo Cement Corp | 熱回収装置及び塩素バイパス設備 |
JP2006305510A (ja) * | 2005-05-02 | 2006-11-09 | Taiheiyo Cement Corp | 燃焼排ガス処理装置及び湿式集塵機排水処理方法 |
WO2009110356A1 (ja) * | 2008-03-07 | 2009-09-11 | 太平洋セメント株式会社 | セメントキルン抽気ガスの処理システム及び処理方法 |
WO2009154088A1 (ja) * | 2008-06-17 | 2009-12-23 | 太平洋セメント株式会社 | セメントキルン排ガスの処理装置及び処理方法 |
JP2009298677A (ja) * | 2008-06-17 | 2009-12-24 | Taiheiyo Cement Corp | セメントキルン抽気ガスの処理システム及び処理方法 |
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JP2009298677A (ja) * | 2008-06-17 | 2009-12-24 | Taiheiyo Cement Corp | セメントキルン抽気ガスの処理システム及び処理方法 |
WO2009154088A1 (ja) * | 2008-06-17 | 2009-12-23 | 太平洋セメント株式会社 | セメントキルン排ガスの処理装置及び処理方法 |
JP2010001176A (ja) * | 2008-06-19 | 2010-01-07 | Taiheiyo Cement Corp | セメントキルン抽気ガスの処理システム及び処理方法 |
JP2015530349A (ja) * | 2012-09-05 | 2015-10-15 | ショイヒ ゲゼルシャフト ミット ベシュレンクテル ハフツング | 揮発性成分を分離するための方法および装置 |
US9957195B2 (en) | 2012-09-05 | 2018-05-01 | Scheuch Gmbh | Process and device for separating off a volatile component |
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JP2014171986A (ja) * | 2013-03-11 | 2014-09-22 | Taiheiyo Cement Corp | 排ガス中の水銀回収方法 |
JP2014177364A (ja) * | 2013-03-14 | 2014-09-25 | Taiheiyo Cement Corp | セメントキルン排ガスの処理装置及び処理方法 |
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KR20190104862A (ko) * | 2017-01-11 | 2019-09-11 | 다이헤이요 엔지니어링 가부시키가이샤 | 시멘트 킬른 배기 가스의 수은 저감 방법 및 그 장치 |
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Also Published As
Publication number | Publication date |
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JPWO2005005025A1 (ja) | 2007-09-20 |
EP1649922A4 (en) | 2006-10-11 |
JP2011056500A (ja) | 2011-03-24 |
DE602004031231D1 (de) | 2011-03-10 |
ES2357647T3 (es) | 2011-04-28 |
WO2005005025B1 (ja) | 2005-03-17 |
EP1649922A1 (en) | 2006-04-26 |
CN1812828A (zh) | 2006-08-02 |
US20070086930A1 (en) | 2007-04-19 |
TWI336269B (en) | 2011-01-21 |
JP4615443B2 (ja) | 2011-01-19 |
US7799297B2 (en) | 2010-09-21 |
TW200510057A (en) | 2005-03-16 |
KR20060029135A (ko) | 2006-04-04 |
DK1649922T3 (da) | 2011-04-04 |
EP1649922B1 (en) | 2011-01-26 |
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