WO2009110356A1 - Système et procédé de traitement de gaz de prélèvement issu d'un four à ciment - Google Patents

Système et procédé de traitement de gaz de prélèvement issu d'un four à ciment Download PDF

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Publication number
WO2009110356A1
WO2009110356A1 PCT/JP2009/053323 JP2009053323W WO2009110356A1 WO 2009110356 A1 WO2009110356 A1 WO 2009110356A1 JP 2009053323 W JP2009053323 W JP 2009053323W WO 2009110356 A1 WO2009110356 A1 WO 2009110356A1
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WO
WIPO (PCT)
Prior art keywords
gas
heat exchanger
extraction
cement kiln
kiln
Prior art date
Application number
PCT/JP2009/053323
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English (en)
Japanese (ja)
Inventor
淳一 寺崎
紳一郎 齋藤
Original Assignee
太平洋セメント株式会社
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Filing date
Publication date
Application filed by 太平洋セメント株式会社 filed Critical 太平洋セメント株式会社
Priority to CN2009801066215A priority Critical patent/CN101959824A/zh
Priority to JP2010501859A priority patent/JPWO2009110356A1/ja
Publication of WO2009110356A1 publication Critical patent/WO2009110356A1/fr

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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
    • B01D53/8678—Removing components of undefined structure
    • B01D53/8687—Organic components
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/004—Systems for reclaiming waste heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/708—Volatile organic compounds V.O.C.'s

Definitions

  • the present invention relates to a processing system and processing method for a cement kiln extraction gas, and in particular, removes organic pollutants contained in the extraction gas extracted from the kiln exhaust gas flow path from the bottom of the cement kiln to the bottom cyclone.
  • a processing system and the like related to a processing system and the like.
  • a chlorine bypass system for extracting a part of combustion gas and removing chlorine from the kiln exhaust gas flow path is used.
  • Chlorine bypass exhaust may also contain persistent organic pollutants (POPs) such as dioxins (PCDD, PCDF, co-PCB), polychlorinated biphenyls (PCBs), and volatile organic pollutants (VOC).
  • POPs persistent organic pollutants
  • PCDD dioxins
  • PCDF polychlorinated biphenyls
  • VOC volatile organic pollutants
  • the present invention has been made in view of the above problems in the prior art, and minimizes poisoning of the catalyst by acid gas when purifying the cement kiln extraction gas using a catalyst device. Meanwhile, an object is to efficiently remove organic pollutants contained in the extracted gas.
  • the present invention is a cement kiln extraction gas processing system, and an extraction means for extracting a part of combustion gas from a kiln exhaust gas passage from the bottom of the cement kiln to the lowermost cyclone.
  • a first heat exchanger that recovers heat while cooling the extraction gas extracted by the extraction unit, a separation unit that separates dust from the extraction gas cooled by the first heat exchanger, and the first
  • a second heat exchanger that heats the extraction gas from which the dust has been separated using heat recovered by the heat exchanger
  • a catalyst device that removes organic pollutants from the extraction gas heated by the second heat exchanger It is characterized by providing.
  • Organic pollutants refer to residual organic pollutants (POPs) such as dioxins (PCDD, PCDF, co-PCB), polychlorinated biphenyls (PCBs), and volatile organic pollutants (VOC).
  • the poisoning of the catalyst by acidic gas is restrained low. Can do.
  • the cooled extraction gas is reheated by the second heat exchanger, adjusted to a temperature suitable for decomposition of the organic pollutant, and then introduced into the catalyst device, so that the organic pollutant is efficiently removed. Is possible.
  • the extraction gas can be heated by effectively using the recovered heat amount, thereby reducing the operation cost. It is also possible to plan.
  • the separation means can be constituted by a dry dust collector, and is cooled by the first heat exchanger between the dry dust collector and the first heat exchanger.
  • An adding means for adding a desulfurizing agent to the extracted gas can also be provided.
  • the addition means when the addition means is provided, the acidic gas in the extracted gas can be more reliably removed, and the poisoning of the catalyst by the acidic gas can be minimized.
  • the separation means can be constituted by a wet dust collector, whereby the acidic gas in the extraction gas can be more reliably removed, and the catalyst is covered with the acidic gas. Poison can be minimized.
  • the first heat exchanger can be constituted by a corrosion-resistant heat exchanger whose inner wall is subjected to a corrosion-resistant treatment, and a dust collector and the like after the first heat exchanger are also included. Corrosion-resistant treatment can be performed. As the corrosion resistance treatment, a coating such as a fluororesin can be used.
  • the present invention is a method for treating a cement kiln extraction gas, wherein a part of the combustion gas is extracted from a kiln exhaust gas flow path from the bottom of the cement kiln to the bottom cyclone, and the extracted extraction gas is Heat is recovered while cooling with the first heat exchanger, dust is separated from the cooled extracted gas, and the extracted gas from which the dust has been separated is introduced into the second heat exchanger, and the first heat exchanger
  • the heat extracted in step (b) is used for heating, and the heated extraction gas is introduced into the catalyst device to remove organic pollutants from the extraction gas.
  • poisoning of the catalyst by acidic gas can be minimized, and organic pollutants in the chlorine bypass exhaust can be efficiently removed.
  • the extraction gas extracted can be cooled to 200 ° C. or less by the first heat exchanger, and according to this, the sulfur oxide in the extraction gas is efficiently removed. And more heat can be recovered from the first heat exchanger.
  • the minimum of cooling will be about 20 degreeC which is normal temperature.
  • the extraction gas from which the dust has been separated can be heated to 150 ° C. or more and 500 ° C. or less by the second heat exchanger. It is possible to efficiently decompose and remove harmful pollutants in the gas.
  • the temperature of the extraction gas is less than 150 ° C., it is difficult to desire a sufficient decomposition rate of harmful pollutants, and when it is higher than 500 ° C., there is a problem that the catalyst life is adversely affected.
  • the cement kiln extraction gas when the cement kiln extraction gas is purified using the catalyst device, it is possible to minimize the poisoning of the catalyst by the acid gas, and the organic contamination contained in the extraction gas. Substances can be removed efficiently.
  • FIG. 1 shows a first embodiment of a cement kiln extraction gas processing system according to the present invention.
  • This processing system 1 is roughly composed of a gas extraction unit 2 and a gas processing unit 3.
  • the gas extraction unit 2 is a facility for extracting a part of the combustion gas from the kiln exhaust gas flow path from the bottom of the cement kiln 4 to the lowermost cyclone (not shown).
  • the gas extraction unit 2 separates a probe 5 for extracting combustion gas, a cooling fan 6 for supplying cold air into the probe 5 to quench the extraction gas G1, and coarse dust D1 contained in the extraction gas G1. It is composed of a cyclone 10 as a classifier.
  • the gas processing unit 3 is a facility for removing harmful substances in the extracted gas.
  • the gas processing unit 3 collects the first heat exchanger 11 that cools the extraction gas G2 discharged from the cyclone 10 and the fine dust D2 in the extraction gas G2 that is cooled by the first heat exchanger 11.
  • Bag filter 12, a dust tank 13 for collecting the fine dust D2 discharged from the first heat exchanger 11 and the bag filter 12, an induction fan 16 for inducing the exhaust gas G3 of the bag filter 12, and an induction fan 16 includes a second heat exchanger 17 that heats the exhaust gas G3 attracted by 16, a catalyst device 18 that removes organic pollutants from the exhaust gas G4 heated by the second heat exchanger 17, and the like.
  • the first heat exchanger 11 is provided for cooling the extraction gas G2 and removing the acid gas in the extraction gas G2.
  • cooling the extraction gas G2 it is preferable to cool it to 200 ° C. or less, thereby promoting the reaction between calcium and sulfur contained in the extraction gas and removing sulfur oxides (SOx). Is possible.
  • the blowing device 14 may be installed on the pipe line 11a connecting the first heat exchanger 11 and the bag filter 12, and a desulfurizing agent may be added as necessary.
  • the desulfurizing agent slaked lime, quick lime, calcined cement material (cement material separated from the lowermost cyclone of the preheater, etc.), coal ash or the like can be used.
  • the corrosion-resistant heat exchanger by which coating, such as a fluororesin, was given to the 1st heat exchanger 11 at the inner wall.
  • the second heat exchanger 17 is provided to reheat the exhaust gas G3 in the front stage of the catalyst device 18 and adjust the temperature of the exhaust gas G3 to a temperature suitable for the catalyst activity. Between the 2nd heat exchanger 17 and the 1st heat exchanger 11, the connecting pipe line 17a for circulating a heat medium is provided, and the 2nd heat exchanger 17 is the 1st heat exchange.
  • the exhaust gas G3 is heated using the heat recovered by the vessel 11. When the exhaust gas G3 is heated, it is preferably heated to 150 ° C. or higher and 500 ° C. or lower, whereby the organic pollutant removal efficiency in the catalyst device 18 can be improved.
  • a heater (not shown) or the like may be installed on the connecting pipe line 17a to supplementarily heat the heat medium.
  • the catalyst device 18 is provided for decomposing and removing organic pollutants such as persistent organic pollutants (POPs) and volatile organic pollutants (VOC) contained in the exhaust gas G4.
  • the catalyst device 18 is configured in a honeycomb shape, and can be configured to be relatively small even when a large amount of exhaust gas is processed.
  • any catalyst capable of removing POPs and VOC such as an oxide catalyst such as a titanium / vanadium catalyst, a noble metal catalyst having a noble metal selected from platinum, palladium, rhodium and ruthenium, can be disposed.
  • the upstream titanium / vanadium catalyst efficiently decomposes NOx and the like in addition to POPs and VOC, and the downstream side.
  • a platinum-based catalyst can efficiently remove CO, odor, and the like.
  • the titanium / vanadium catalyst means a catalyst essentially including titanium (Ti) and vanadium (V). This catalyst exhibits a high function for decomposing and removing organic pollutants, and has a high decomposition activity (denitration activity) of NOx, which is a harmful substance.
  • the extraction gas G1 exhausted from the probe 5 is separated into the coarse powder D1 and the gas G2 containing the fine powder D2, and the coarse powder D1 is returned to the cement kiln system while being 250 to 600 ° C.
  • the extracted gas G2 is introduced into the first heat exchanger 11.
  • the sulfur content (SOx) and the acid gas are removed while cooling the extraction gas G2 to 200 ° C. or less.
  • the bag filter 12 the fine powder D2 in the gas G2 is collected and collected in the dust tank 13 as chlorine bypass dust.
  • the exhaust gas G3 of the bag filter 12 is attracted by the attracting fan 16 and reheated to 150 ° C. or more and 500 ° C. or less in the second heat exchanger 17.
  • the heated exhaust gas G4 is introduced into the catalyst device 18, and organic pollutants such as POPs and VOC are decomposed to purify the exhaust gas G4.
  • the exhaust gas G5 purified by the catalyst device 18 may be released to the atmosphere via an exhaust fan (not shown), or may be returned to the cement process for heat recovery.
  • the extraction gas G1 extracted by the probe 5 is cooled by the first heat exchanger 11, and the acidic gas in the extraction gas G1 is removed. 18 poisoning can be suppressed to a low level.
  • the cooled exhaust gas G3 is reheated by the second heat exchanger 17 and adjusted to a temperature suitable for the decomposition of the organic pollutant, and then introduced into the catalyst device 18, so that the organic pollutant is efficiently removed. It becomes possible.
  • the heat recovered by the first heat exchanger 11 is used when the exhaust gas G3 is heated, the exhaust gas G3 can be heated by effectively using the recovered heat amount, thereby reducing the operating cost. It becomes possible.
  • this processing system 20 includes a first heat exchanger 11 that cools the extraction gas G2 in the gas processing unit 3, and a wet extraction gas G2 that is cooled by the first heat exchanger 11.
  • Wet dust collector 21 that collects dust
  • an induction fan 16 that attracts exhaust gas G3 of wet dust collector 21
  • a second heat exchanger 17 that heats exhaust gas G3 attracted by induction fan 16, and a second heat exchanger 17
  • the structure of the gas extraction part 2 is the same as the case of the processing system 1 of FIG.
  • the wet dust collector 21 is provided to collect water-soluble components and dust contained in the extraction gas G2 cooled by the first heat exchanger 11, and includes dust and water-soluble chlorine containing sulfur oxide (SOx) and the like. Collect the compound.
  • a circulating liquid tank 22 is provided below the wet dust collector 21, and a mist separator 23 is disposed on the downstream side of the circulating liquid tank 22.
  • the extraction gas G1 extracted by the probe 5 is cooled to 200 ° C. or less by the first heat exchanger 11, and after removing SOx contained in the extraction gas G2, the extraction gas G1 is further extracted by the wet dust collector 21. Wet dust collection of SOx remaining in the gas G2. Therefore, the acidic gas in the extracted gas G2 can be more reliably removed, and poisoning of the catalyst device 18 by the acidic gas can be minimized.
  • the exhaust gas G3 from the wet dust collector 21 is reheated to 150 ° C. or more and 500 ° C. or less by the second heat exchanger 17, and then the catalyst device 18 is passed through.
  • Organic pollutants such as POPs and VOCs can be efficiently decomposed and removed.
  • the exhaust gas G3 is heated using the heat recovered by the first heat exchanger 11, so that it is possible to reduce the operating cost, as in the first embodiment. The effect of this can be obtained.

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

Abstract

Un gaz de prélèvement issu d'un four à ciment est purifié avec un catalyseur en éliminant avec efficacité les polluants organiques contenus dans le gaz de prélèvement, tout en réduisant au minimum l'altération du catalyseur par un gaz acide. Un système (1) de traitement d'un gaz de prélèvement issu d'un four à ciment comprend : une sonde (5) qui prélève un passage de gaz d'une partie d'un gaz de combustion, passage qui s'évacue du four et qui part du bas d'un four à ciment (4) jusqu'à un cyclone de niveau le plus inférieur; un premier échangeur thermique (11) qui récupère la chaleur tout en refroidissant le gaz de prélèvement (G2) extrait par la sonde (5); un filtre à sac (12) qui sépare la poussière du gaz de prélèvement (G2) refroidi par le premier échangeur thermique (11); un second échangeur thermique (17) grâce auquel le gaz de prélèvement (G3) dont la poussière a été séparée est chauffé avec la chaleur récupérée par le premier échangeur thermique (11); et un dispositif catalyseur (18) qui décompose les polluants organiques contenus dans le gaz de prélèvement (G4) chauffé par le second échangeur thermique (17) et les élimine.
PCT/JP2009/053323 2008-03-07 2009-02-25 Système et procédé de traitement de gaz de prélèvement issu d'un four à ciment WO2009110356A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CN2009801066215A CN101959824A (zh) 2008-03-07 2009-02-25 水泥窑抽出气体之处理系统及处理方法
JP2010501859A JPWO2009110356A1 (ja) 2008-03-07 2009-02-25 セメントキルン抽気ガスの処理システム及び処理方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2008057818 2008-03-07
JP2008-057818 2008-03-07

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WO2009110356A1 true WO2009110356A1 (fr) 2009-09-11

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JP (1) JPWO2009110356A1 (fr)
KR (1) KR20110000620A (fr)
CN (2) CN101959824A (fr)
TW (1) TW200940158A (fr)
WO (1) WO2009110356A1 (fr)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
CN102102944A (zh) * 2009-09-07 2011-06-22 厦门热工环保系统工程有限公司 一种回转窑烟气余热回收方法
JP2011195339A (ja) * 2010-03-17 2011-10-06 Taiheiyo Cement Corp 燃焼ガス抽気プローブ及びその運転方法
JP2012140313A (ja) * 2011-01-06 2012-07-26 Taiheiyo Cement Corp 塩素バイパスシステム及び塩素バイパス抽気ガスの処理方法
JP2012171098A (ja) * 2011-02-17 2012-09-10 Seiko Epson Corp 液体噴射装置
WO2015179892A1 (fr) * 2014-05-27 2015-12-03 Scheuch Gmbh Dispositif de fabrication de clinker
JP2016022439A (ja) * 2014-07-23 2016-02-08 太平洋セメント株式会社 セメントキルン排ガス処理装置及び処理方法
JP2016023108A (ja) * 2014-07-23 2016-02-08 太平洋セメント株式会社 セメントキルン排ガス処理装置及び処理方法
CN106524773A (zh) * 2011-01-31 2017-03-22 太平洋水泥株式会社 氯旁通系统和氯旁通抽气气体的处理方法
JP2017060905A (ja) * 2015-09-24 2017-03-30 太平洋セメント株式会社 セメントキルン排ガス処理装置及び処理方法
WO2019072957A1 (fr) * 2017-10-12 2019-04-18 Thyssenkrupp Industrial Solutions Ag Procédé et installation pour la production d'un clinker de ciment ou d'un autre produit minéral
EP3513885A1 (fr) * 2013-06-07 2019-07-24 Milli Spanovic Installation et procédure de traitement d'un solidificat

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CN103644744B (zh) * 2013-12-25 2015-07-22 巨石集团有限公司 一种窑炉烟气余热梯级利用方法
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KR101985068B1 (ko) * 2017-02-17 2019-05-31 두산중공업 주식회사 열교환기 분진오염 방지 시스템
CN116147371A (zh) * 2023-02-22 2023-05-23 中国中材国际工程股份有限公司 一种提高水泥工业化石燃料替代率的系统及方法
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WO2005005025A1 (fr) * 2003-07-10 2005-01-20 Taiheiyo Cement Corporation Dispositif et procede de traitement des gaz d'echappement de combustion
WO2006073083A1 (fr) * 2005-01-06 2006-07-13 Taiheiyo Cement Corporation Appareil et procede de traitement d’un effluent gazeux de combustion de four a ciment
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Publication number Priority date Publication date Assignee Title
JP2002219335A (ja) * 2001-01-30 2002-08-06 Babcock Hitachi Kk 排ガス処理装置
WO2005005025A1 (fr) * 2003-07-10 2005-01-20 Taiheiyo Cement Corporation Dispositif et procede de traitement des gaz d'echappement de combustion
WO2006073083A1 (fr) * 2005-01-06 2006-07-13 Taiheiyo Cement Corporation Appareil et procede de traitement d’un effluent gazeux de combustion de four a ciment
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

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
CN102102944A (zh) * 2009-09-07 2011-06-22 厦门热工环保系统工程有限公司 一种回转窑烟气余热回收方法
JP2011195339A (ja) * 2010-03-17 2011-10-06 Taiheiyo Cement Corp 燃焼ガス抽気プローブ及びその運転方法
JP2012140313A (ja) * 2011-01-06 2012-07-26 Taiheiyo Cement Corp 塩素バイパスシステム及び塩素バイパス抽気ガスの処理方法
CN106524773A (zh) * 2011-01-31 2017-03-22 太平洋水泥株式会社 氯旁通系统和氯旁通抽气气体的处理方法
JP2012171098A (ja) * 2011-02-17 2012-09-10 Seiko Epson Corp 液体噴射装置
EP3513885A1 (fr) * 2013-06-07 2019-07-24 Milli Spanovic Installation et procédure de traitement d'un solidificat
WO2015179892A1 (fr) * 2014-05-27 2015-12-03 Scheuch Gmbh Dispositif de fabrication de clinker
JP2016022439A (ja) * 2014-07-23 2016-02-08 太平洋セメント株式会社 セメントキルン排ガス処理装置及び処理方法
JP2016023108A (ja) * 2014-07-23 2016-02-08 太平洋セメント株式会社 セメントキルン排ガス処理装置及び処理方法
JP2017060905A (ja) * 2015-09-24 2017-03-30 太平洋セメント株式会社 セメントキルン排ガス処理装置及び処理方法
WO2019072957A1 (fr) * 2017-10-12 2019-04-18 Thyssenkrupp Industrial Solutions Ag Procédé et installation pour la production d'un clinker de ciment ou d'un autre produit minéral

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TW200940158A (en) 2009-10-01

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