WO2012120933A1 - Dispositif et procédé de traitement des gaz d'échappement par dérivation du chlore - Google Patents

Dispositif et procédé de traitement des gaz d'échappement par dérivation du chlore Download PDF

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Publication number
WO2012120933A1
WO2012120933A1 PCT/JP2012/051519 JP2012051519W WO2012120933A1 WO 2012120933 A1 WO2012120933 A1 WO 2012120933A1 JP 2012051519 W JP2012051519 W JP 2012051519W WO 2012120933 A1 WO2012120933 A1 WO 2012120933A1
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WIPO (PCT)
Prior art keywords
exhaust gas
chlorine bypass
solid
gas
liquid separation
Prior art date
Application number
PCT/JP2012/051519
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English (en)
Japanese (ja)
Inventor
淳一 寺崎
鈴木　崇幸
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太平洋セメント株式会社
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Publication of WO2012120933A1 publication Critical patent/WO2012120933A1/fr

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
    • 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
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • 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
    • F27D17/008—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
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/604—Hydroxides
    • 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
    • B01D2257/302—Sulfur oxides
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/20—Sulfur; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/50—Intercepting solids by cleaning fluids (washers or scrubbers)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/60—Intercepting solids using settling/precipitation chambers

Definitions

  • the present invention relates to an apparatus and a method for treating gas discharged from a chlorine bypass facility for extracting chlorine from a kiln exhaust gas passage from a kiln bottom of a cement kiln to a lowermost cyclone to remove chlorine.
  • a chlorine bypass facility for extracting chlorine from a kiln exhaust gas passage from a kiln bottom of a cement kiln to a lowermost cyclone to remove chlorine.
  • a chlorine bypass facility for extracting a part of combustion gas and removing chlorine is used.
  • the chlorine bypass facility includes a probe 53 for extracting a part of combustion gas from a kiln exhaust gas flow path from the bottom of the kiln 52 to the lowermost cyclone (not shown), and a probe 53.
  • a cooling fan 54 for rapidly cooling the extraction gas G1 by supplying cold air therein, a cyclone 55 as a classifier for separating the coarse dust D1 contained in the extraction gas G1, and a fine powder D2 discharged from the cyclone 55
  • a cooler 56 that cools the extracted gas G2, a cooling fan 57 that supplies cool air to the cooler 56, a bag filter 58 that collects dust dust D2 in the extracted gas G2 cooled by the cooler 56, and cooling
  • a dust tank 59 for collecting the fine powder D2 discharged from the vessel 56 and the bag filter 58, a dissolution tank 60 for dissolving the fine powder D2 from the dust tank 59 in water,
  • a solid-liquid separation device 61 for solid-liquid separation of the slurry S1 from the cracking tank 60
  • the present invention was made in view of the problems in the above-described conventional technology, and the gas discharged from the chlorine bypass facility (chlorine bypass exhaust gas) without increasing the heat loss of the cement firing system,
  • the objective is to process at low cost while ensuring stable operation of the cement firing system.
  • the present invention is a chlorine bypass exhaust gas treatment apparatus, which bleeds while cooling a part of combustion gas from a kiln exhaust gas passage from a kiln bottom of a cement kiln to a lowermost cyclone.
  • a desulfurization tower for desulfurization of the exhaust gas by contacting the exhaust gas with the exhaust gas of the chlorine bypass facility.
  • chlorine bypass dust by adding an alkali agent to the chlorine bypass dust, varying the CaCl 2 and CaCO 3 contained in the chlorine bypass dust to Ca (OH) 2, chlorine bypass the Ca (OH) 2 Since it is used for desulfurization of equipment exhaust gas, calcium contained in chlorine bypass dust can be effectively used for desulfurization, and stable operation of the cement firing system is ensured without increasing the heat loss of the cement firing system.
  • the chlorine bypass exhaust gas can be treated at a low cost.
  • the chlorine content of the re-dissolved slurry is low, and it is possible to minimize the dissolution of gypsum causing scale trouble, It is possible to suppress the production of singenite (K 2 Ca (SO 4 ) 2 ) or the like that hinders the effective use of the recovered material.
  • lead (Pb) and selenium (Se) among the heavy metals contained in the chlorine bypass dust are contained in the filtrate side by adding an alkali agent. Since selenium is included in the recovered industrial salt, there is no problem, so that lead and selenium can be efficiently removed from the chlorine bypass dust.
  • a second solid-liquid separation device for solid-liquid separation of the slurry discharged from the desulfurization tower, and a filtrate solid-liquid separated by the second solid-liquid separation device are used for the second treatment.
  • a sulfiding agent and a pH adjuster are added to the filtrate separated by solid-liquid separation in the first solid-liquid separation device, and an adjustment tank is provided that insolubilizes heavy metals contained in the filtrate. Can do. As a result, lead or the like can be insolubilized and efficiently recovered at a later stage.
  • the chlorine bypass exhaust gas treatment apparatus may include a third solid-liquid separation device for solid-liquid separation of the filtrate discharged from the adjustment tank. As a result, heavy metals such as lead can be recovered on the cake side.
  • the chlorine bypass exhaust gas treatment apparatus may further include a salt recovery device that recovers salt from the filtrate discharged from the third solid-liquid separation device, and further, heat recovered from the extracted gas is supplied to the salt recovery device.
  • a gas gas heater used for salt recovery can be provided. Thereby, salt can be recovered while effectively using the heat of the chlorine bypass exhaust gas.
  • the gas gas heater can recover heat from the exhaust gas of a high-temperature dust collector that collects the extracted gas, and heat efficiency is improved by recovering heat from the removed high-temperature gas.
  • the present invention is a method for treating chlorine bypass exhaust gas, wherein a part of the combustion gas is extracted from the kiln exhaust gas flow path from the bottom of the kiln of the cement kiln to the lowest cyclone, and extracted from the extracted gas.
  • a chlorine bypass facility for recovering chlorine bypass dust after slurrying while adding an alkali agent to the recovered chlorine bypass dust, the slurry is dehydrated, the resulting cake is redissolved, and the cake is redissolved The slurry is brought into contact with the exhaust gas of the chlorine bypass facility, and the exhaust gas is desulfurized.
  • the present invention similarly to the above-described invention, it is possible to treat the chlorine bypass exhaust gas by effectively using calcium contained in the chlorine bypass dust for desulfurization, and minimize the dissolution of gypsum causing scale trouble.
  • lead and selenium can be efficiently removed from the chlorine bypass dust.
  • the pH of the slurry can be adjusted to 13 or more and 14 or less, and CaCl 2 and CaCO 3 contained in the chlorine bypass dust are efficiently changed to Ca (OH) 2 in this pH region. Can be made.
  • chlorine bypass exhaust gas can be processed at low cost while ensuring stable operation of the cement firing system without increasing the heat loss of the cement firing system.
  • FIG. 1 shows a chlorine bypass facility provided with a first embodiment of a chlorine bypass exhaust gas treatment apparatus according to the present invention.
  • the chlorine bypass facility 1 is arranged from the kiln bottom of a cement kiln 2 to a lowermost cyclone (not shown).
  • a probe 3 for extracting a part of the combustion gas while being cooled by cold air from the cooling fans 4 and 5, and coarse dust of dust contained in the extracted gas G1 extracted by the probe 3 A cyclone 6 that separates D1, a cooler 7 that cools the extracted gas G2 containing fine powder D2 discharged from the cyclone 6, a bag filter 8 that collects the extracted gas G3 from the cooler 7, and a bag filter 8
  • a desulfurization tower 11 that performs a desulfurization treatment of the exhaust gas G4 supplied through the fan 10 and a dust D5 (D3 + D4) discharged from the cooler 7 and the bag filter 8 are stored.
  • the solid tank 9, the first dissolution tank 12 that is slurried while adding an alkali agent to the dust (chlorine bypass dust) D 6 discharged from the dust tank 9, and the slurry S 1 discharged from the first dissolution tank 12 are solidified.
  • the first solid-liquid separation device 13 for liquid separation, the second solid-liquid separation device 15 for solid-liquid separation of the slurry S3 generated in the desulfurization tower 11, and the cake C1 discharged from the first solid-liquid separation device 13 Is dissolved in the filtrate L2 (circulated water CW) from the second solid-liquid separator 15 and the filtrate L1 discharged from the first solid-liquid separator 13 is added with a sulfiding agent and pH adjustment.
  • the first dissolution tank 12 slurries the dust D6 from the dust tank 9 using water (or hot water) and adds an alkali agent such as NaOH to convert CaCl 2 and CaCO 3 contained in the dust D6 into Ca. Provided to change to (OH) 2 .
  • the first solid-liquid separator 13 is provided for solid-liquid separation of the slurry S1 discharged from the first dissolution tank 12.
  • the cake C1 subjected to the solid-liquid separation is supplied to the second dissolution tank 14, and the filtrate L1 is supplied to the adjustment tank 16.
  • the second dissolution tank 14 is provided for re-dissolving the cake C1 discharged from the first solid-liquid separator 13, and the slurry S2 obtained by dissolving the cake C1 in the circulating water CW is a bug in the desulfurization tower 11. It is used for desulfurization of the exhaust gas G4 of the filter 8.
  • the desulfurization tower 11 is provided to desulfurize the exhaust gas G4 supplied from the bag filter 8 via the fan 10 using the slurry S2 supplied from the second dissolution tank 14.
  • the slurry S3 containing dihydrate gypsum generated by the desulfurization is returned to the second solid-liquid separator 15, and the desulfurized exhaust gas G5 is returned to the exhaust gas system of the cement kiln 2.
  • the second solid-liquid separation device 15 is provided for solid-liquid separation of the slurry S3 supplied from the desulfurization tower 11, and the filtrate L2 obtained by solid-liquid separation is recirculated in the second dissolution tank 14 as circulating water CW. Used. On the other hand, dihydrate gypsum Gy is recovered on the cake C2 side where the solid-liquid separation is performed.
  • the adjustment tank 16 is provided to add a sulfurizing agent such as NaSH or a pH adjusting agent to the filtrate L1 discharged from the first solid-liquid separation device 13 so as to insolubilize heavy metals such as lead.
  • a sulfurizing agent such as NaSH or a pH adjusting agent
  • a pH adjuster NaOH, Ca (OH) 2 , CaO, Mg (OH) 2 , sulfuric acid or the like can be used.
  • the third solid-liquid separation device 17 is provided for solid-liquid separation of the filtrate L3 discharged from the adjustment tank 16, and industrial salt may be recovered from the filtrate L4 subjected to solid-liquid separation by a salt recovery device, Waste water can also be treated. Further, heavy metals such as lead are recovered on the cake C3 side where the solid-liquid separation is performed.
  • the extraction gas G2 containing the fine powder D2 separated by the cyclone 6 is introduced into the cooler 7, and heat exchange between the extraction gas G2 and the medium is performed.
  • the extracted gas G3 cooled by heat exchange is introduced into the bag filter 8, and the bag filter 8 collects the dust D4 contained in the extracted gas G3.
  • the dust D4 collected by the bag filter 8 is temporarily stored in the dust tank 9 as the dust D5 together with the dust D3 discharged from the cooler 7, and is introduced into the first dissolution tank 12 as the dust D6.
  • the dust D6 introduced into the first dissolution tank 12 is mixed with water (or warm water) and an alkaline agent such as NaOH in the first dissolution tank 12 to generate a slurry S1.
  • an alkaline agent such as NaOH in the first dissolution tank 12
  • the pH in the first dissolution tank 12 is adjusted to 13.5 ⁇ 0.5.
  • CaCl 2 and CaCO 3 contained in the dust D6 react with the alkali agent to generate Ca (OH) 2 , and these calcium components can be effectively used for desulfurization in the desulfurization tower 11 at the subsequent stage.
  • KOH or the like can be used in addition to NaOH.
  • the slurry S1 discharged from the first dissolution tank 12 is subjected to solid-liquid separation by the first solid-liquid separation device 13, and the cake obtained by solid-liquid separation while solid-liquid separation of the slurry S1 is washed with water.
  • Remove chlorine The cake C1 from which the chlorine content has been removed is supplied to the second dissolution tank 14 and the re-dissolved slurry S2 is supplied to the desulfurization tower 11 and used for desulfurization.
  • the exhaust gas G5 after desulfurization is introduced into the exhaust gas system of the cement kiln 2.
  • Ca (OH) 2 present in the re-dissolved slurry S2 reacts with SO 2 contained in the exhaust gas G4 of the bag filter 8 in the desulfurization tower 11, and dihydrate gypsum (CaSO 4 .2H 2 O). Converted to At this time, since the potassium and chlorine contents were removed in the first solid-liquid separator 13, the chlorine content of the slurry S2 obtained by re-dissolving the cake C1 is low, and the dissolution of gypsum causing scale trouble is minimized. In addition, it is possible to suppress the formation of singenite (K 2 Ca (SO 4 ) 2 ). In addition, when syngenite is added to cement, the production must be suppressed because it affects cement quality, particularly strength.
  • the slurry S3 discharged from the desulfurization tower 11 is solid-liquid separated by the second solid-liquid separator 15 and the dihydrate gypsum Gy obtained on the cake C2 side is pulverized together with the cement clinker by a cement mill to produce cement. Can be used.
  • the separated filtrate L2 can be reused for the production of the slurry S2 in the second dissolution tank 14 as the circulating water CW.
  • the filtrate L1 solid-liquid separated by the first solid-liquid separator 13 is supplied to the adjustment tank 16, and a sulfurizing agent such as NaSH or a pH adjuster is added to the filtrate L1 to precipitate heavy metals such as lead. Then, the solid-liquid separation is performed by the third solid-liquid separation device 17 to recover the heavy metal on the cake C3 side. If necessary, a filter aid is added before the filtrate L3 is supplied to the third solid-liquid separator 17. Further, industrial salt may be recovered from the filtrate L4 subjected to solid-liquid separation by the third solid-liquid separation device 17, and the filtrate L4 may be discharged after the waste water treatment. When the industrial salt is recovered, CaCl 2 is changed to Ca (OH) 2 as described above, so that an industrial salt having a low calcium concentration and a high KCl content can be obtained.
  • a sulfurizing agent such as NaSH or a pH adjuster
  • the chlorine bypass facility 31 includes a high-temperature dust collector 32 instead of the cooler 7 and the bag filter 8 of the chlorine bypass facility 1, and a gas gas heater 33 is disposed at the subsequent stage of the high-temperature dust collector 32, and the atmosphere heated by the gas gas heater 33. Is used for salt recovery. Since the other components of the chlorine bypass facility 31 are the same as those of the chlorine bypass facility 1 shown in FIG. 1, the same reference numerals are given and description thereof is omitted.
  • the high-temperature dust collector 32 is, for example, a heat-resistant bag filter having a heat resistance up to about 900 ° C. or a high-temperature processing type electric dust collector having a heat resistance up to about 900 ° C., and the fine dust D2 discharged from the cyclone 6 is collected.
  • the extracted gas G2 is collected without cooling, and the collected dust (chlorine bypass dust) D3 is supplied to the dust tank 9.
  • the gas gas heater 33 is provided to heat the air A1 taken from the surroundings by the extracted gas G3 discharged from the high temperature dust collector 32 and to use the high temperature air A2 heated by the gas gas heater 33 for subsequent salt recovery. Further, the heat exchange with the air A2 enables the temperature of the exhaust gas G4 to be desulfurized in the desulfurization tower 11 to be adjusted, and the occurrence of consolidation can be suppressed. Further, the heat recovered by the gas gas heater 33 may be used for raising the temperature of the exhaust gas G5 in the desulfurization tower 11.
  • the extraction gas G2 containing the fine powder D2 separated by the cyclone 6 is introduced into the high temperature dust collector 32, the dust D2 contained in the extraction gas G2 is collected in the high temperature dust collector 32, and the dust D3 discharged from the high temperature dust collector 32 is collected. Is temporarily stored in the dust tank 9 and introduced into the first dissolution tank 12 as dust D4.
  • the air A1 taken from the surroundings and the exhaust gas G3 of the high temperature dust collector 32 are introduced into the gas gas heater 33, and after heat exchange between them, the high temperature air A2 is used for salt recovery and discharged from the gas gas heater 33.
  • the exhaust gas G4 is introduced into the desulfurization tower 11 and then desulfurized. Other flows are the same as in the case of the chlorine bypass facility 1.
  • the chlorine bypass exhaust gas treatment apparatus has the same effect as that of the first embodiment, and uses the sensible heat of the chlorine bypass exhaust gas for salt recovery. Can be reduced.

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Abstract

La présente invention concerne le traitement de gaz d'échappement par dérivation du chlore, d'un coût faible, n'entraînant pas de perte de chaleur supplémentaire au niveau d'un système de production de ciment tout en assurant un fonctionnement sans danger de celui-ci. L'invention concerne donc un dispositif de traitement des gaz d'échappement par dérivation du chlore associé à un système de dérivation du chlore (1) qui refroidit et extrait une partie (G) d'un gaz de combustion sortant du conduit d'échappement d'un four depuis le fond d'un four à ciment (2) en direction d'un hydrocyclone inférieur et qui récupère la poussière de dérivation du chlore (D6) en provenance du gaz d'extraction (G1), ledit dispositif comprenant une première cuve de dissolution (12) pour la mise en suspension de la poussière de dérivation du chlore recueillie à laquelle est ajouté un agent alcalin ; un dispositif de séparation solide/liquide (13) qui permet de séparer les solides et les liquides d'une suspension (S1) formée dans la première cuve de dissolution ; une seconde cuve de dissolution (14) permettant de dissoudre une nouvelle fois un tourteau (C1) formé dans le dispositif de séparation solide/liquide ; et une tour de désulfuration (11) permettant de mettre en contact une suspension (S2) formée dans la seconde cuve de dissolution, après sa redissolution, avec les gaz d'échappement (G4) du système de dérivation du chlore et de désulfurer ainsi les gaz d'échappement.
PCT/JP2012/051519 2011-03-09 2012-01-25 Dispositif et procédé de traitement des gaz d'échappement par dérivation du chlore WO2012120933A1 (fr)

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JP2011-051103 2011-03-09
JP2011051103A JP5680450B2 (ja) 2011-03-09 2011-03-09 塩素バイパス排ガスの処理装置及び処理方法

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TW (1) TWI547306B (fr)
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CN106669397A (zh) * 2015-11-05 2017-05-17 宁夏琪凯节能设备有限公司 一种节能型废气治理设备
JP2020001963A (ja) * 2018-06-28 2020-01-09 宇部興産株式会社 セメント組成物の製造方法、及びセメント組成物の製造システム

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JP6012071B2 (ja) * 2012-12-03 2016-10-25 太平洋セメント株式会社 塩素バイパス排ガスの処理方法
WO2015046200A1 (fr) * 2013-09-25 2015-04-02 太平洋セメント株式会社 Procédé de traitement de gaz extrait d'un four à ciment, système de dérivation du chlore et dispositif de cuisson du ciment
DE102014116532A1 (de) * 2014-11-12 2016-05-12 Thyssenkrupp Ag Verfahren zur Verminderung eines Schadstoffgehalts eines bei einer thermischen Behandlung eines Materials entstehenden oder genutzten Abgasstroms
CN106000045B (zh) * 2016-06-17 2019-04-16 王骞 锅炉烟气深度除尘脱硫脱硝设备
KR101998997B1 (ko) * 2017-12-21 2019-07-10 현대제철 주식회사 소결 배가스 분진 불순물 제거 방법

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WO2012020691A1 (fr) * 2010-08-10 2012-02-16 太平洋セメント株式会社 Procédé et dispositif pour le traitement de la poussière de dérivation du chlore et de gaz d'échappement

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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
WO2012020691A1 (fr) * 2010-08-10 2012-02-16 太平洋セメント株式会社 Procédé et dispositif pour le traitement de la poussière de dérivation du chlore et de gaz d'échappement

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CN106669397A (zh) * 2015-11-05 2017-05-17 宁夏琪凯节能设备有限公司 一种节能型废气治理设备
JP2020001963A (ja) * 2018-06-28 2020-01-09 宇部興産株式会社 セメント組成物の製造方法、及びセメント組成物の製造システム

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