WO2012120933A1 - Device and method for processing chlorine bypass exhaust gas - Google Patents

Device and method for processing chlorine bypass exhaust gas 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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Prior art keywords
exhaust gas
chlorine bypass
solid
gas
liquid separation
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PCT/JP2012/051519
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French (fr)
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/en

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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

[Problem] To process chlorine bypass exhaust gas at low cost without increasing heat loss of a cement burning system while ensuring safe operation of the cement burning system. [Solution] A device for processing chlorine bypass exhaust gas associated with a chlorine bypass system (1) which cools and extracts a part (G) of a combustion gas from a kiln exhaust gas passage from the kiln bottom of a cement kiln (2) to a lowermost cyclone and which recovers chlorine bypass dust (D6) from extraction gas (G1), the device comprising: a first dissolution tank (12) for slurrying the recovered chlorine bypass dust while adding an alkali agent thereto; a solid-liquid separation device (13) for separating solids and liquids in a slurry (S1) generated in the first dissolution tank; a second dissolution tank (14) for redissolving a cake (C1) generated in the solid-liquid separation device; and a desulfurization tower (11) for contacting a slurry (S2) after redissolution generated in the second dissolution tank with an exhaust gas (G4) of the chlorine bypass system and desulfurizing the exhaust gas.

Description

塩素バイパス排ガスの処理装置及び処理方法Chlorine bypass exhaust gas treatment device and treatment method
　本発明は、セメントキルンの窯尻から最下段サイクロンに至るまでのキルン排ガス流路より、燃焼ガスの一部を抽気して塩素を除去する塩素バイパス設備から排出されるガスを処理する装置及び方法に関する。 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. About.
　従来、セメント製造設備におけるプレヒータの閉塞等の問題を引き起こす原因となる塩素、硫黄、アルカリ等の中で、塩素が特に問題となることに着目し、セメントキルンの窯尻から最下段サイクロンに至るまでのキルン排ガス流路より、燃焼ガスの一部を抽気して塩素を除去する塩素バイパス設備が用いられている。 Focusing on chlorine, sulfur, alkali, etc., which causes problems such as blockage of preheaters in cement manufacturing facilities, from the bottom of the kiln kiln to the bottom cyclone From the kiln exhaust gas flow path, a chlorine bypass facility for extracting a part of combustion gas and removing chlorine is used.
　塩素バイパス設備は、図３に示すように、セメントキルン５２の窯尻から最下段サイクロン（不図示）に至るまでのキルン排ガス流路より、燃焼ガスの一部を抽気するプローブ５３と、プローブ５３内に冷風を供給して抽気ガスＧ１を急冷する冷却ファン５４と、抽気ガスＧ１に含まれるダストの粗粉Ｄ１を分離する分級機としてのサイクロン５５と、サイクロン５５から排出された微粉Ｄ２を含む抽気ガスＧ２を冷却する冷却器５６と、冷却器５６に冷風を供給する冷却ファン５７と、冷却器５６で冷却された抽気ガスＧ２中のダストの微粉Ｄ２を集塵するバグフィルタ５８と、冷却器５６及びバグフィルタ５８から排出された微粉Ｄ２を回収するダストタンク５９と、ダストタンク５９からの微粉Ｄ２を水に溶解させる溶解槽６０と、溶解槽６０からのスラリーＳ１を固液分離して水洗ケークＣと排水Ｌとに固液分離する固液分離装置６１とを備え、固液分離された水洗ケークＣ及び排水処理後の残渣Ｒをキルン系へ戻し、排水Ｌを排水処理後に放流する。 As shown in FIG. 3, 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 into solid-liquid separation into a water-washed cake C and waste water L is provided. Return to the kiln system and discharge the waste water L after waste water treatment.
　上記塩素バイパス設備５１では、バグフィルタ５８の排ガスＧ３に多量のＳＯ2が含まれるため、この排ガスＧ３をそのまま系外へ放出することができず、排気ファン（不図示）を介してキルン系に戻していた。この際、排ガスＧ３をセメントキルン５２の排ガスを誘引するファン（ＩＤＦ）の出口側に戻すと、煙突から大気に放出される排ガス中のＳＯ2が増加するという問題がある。また、上記排ガスＧ３をセメントキルン５２に付設されるプレヒータに戻すと、セメント焼成系の熱損失の増加、及びクリンカ生産量の低下を招くと共に、硫黄分の濃縮によるコーチングトラブルなどを引き起こすという問題がある。 In the chlorine bypass facility 51, since a large amount of SO 2 is contained in the exhaust gas G3 of the bag filter 58, the exhaust gas G3 cannot be discharged out of the system as it is, and a kiln system is provided via an exhaust fan (not shown). I was returning. At this time, if the exhaust gas G3 is returned to the outlet side of the fan (IDF) for attracting the exhaust gas from the cement kiln 52, there is a problem that SO 2 in the exhaust gas released from the chimney to the atmosphere increases. Moreover, when the exhaust gas G3 is returned to the preheater attached to the cement kiln 52, there is a problem that the heat loss of the cement firing system and the clinker production amount are reduced, and that the trouble of coaching due to the concentration of sulfur is caused. is there.
　そこで、本発明は、上記従来の技術における問題点に鑑みてなされたものであって、塩素バイパス設備から排出されるガス（塩素バイパス排ガス）を、セメント焼成系の熱損失を増加させることなく、セメント焼成系の安定運転を確保しながら、低コストで処理することを目的とする。 Therefore, 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.
　上記目的を達成するため、本発明は、塩素バイパス排ガスの処理装置であって、セメントキルンの窯尻から最下段サイクロンに至るまでのキルン排ガス流路より燃焼ガスの一部を冷却しながら抽気し、該抽気ガスから塩素バイパスダストを回収する塩素バイパス設備に付設され、前記回収された塩素バイパスダストにアルカリ剤を添加しながらスラリー化する第１の溶解槽と、該第１の溶解槽で生成されたスラリーを固液分離する固液分離装置と、該固液分離装置で生成されたケークを再溶解させる第２の溶解槽と、前記第２の溶解槽で生成された再溶解後のスラリーを該塩素バイパス設備の排ガスに接触させ、該排ガスの脱硫を行う脱硫塔とを備えることを特徴とする。 In order to achieve the above-mentioned object, 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 first dissolution tank attached to a chlorine bypass facility for recovering chlorine bypass dust from the extracted gas, and slurried while adding an alkaline agent to the recovered chlorine bypass dust, and produced in the first dissolution tank A solid-liquid separation device for solid-liquid separation of the formed slurry, a second dissolution tank for re-dissolving the cake generated in the solid-liquid separation device, and a slurry after re-dissolution generated in the second dissolution tank And a desulfurization tower for desulfurization of the exhaust gas by contacting the exhaust gas with the exhaust gas of the chlorine bypass facility.
　そして、本発明によれば、塩素バイパスダストにアルカリ剤を添加することで、塩素バイパスダストに含まれるＣａＣｌ2及びＣａＣＯ3をＣａ（ＯＨ）2に変化させ、このＣａ（ＯＨ）2を塩素バイパス設備の排ガスの脱硫に利用するため、塩素バイパスダストに含まれるカルシウム分を脱硫に有効に利用することができ、セメント焼成系の熱損失の増加を招くことなく、セメント焼成系の安定運転を確保しながら、低コストで塩素バイパス排ガスを処理することができる。 Then, according to the present invention, 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. However, the chlorine bypass exhaust gas can be treated at a low cost.
　また、固液分離装置においてスラリー中のカリウム分や塩素分を除去するため、再溶解したスラリーの塩素含有率が低く、スケールトラブルの原因となる石膏の溶解を最小限に抑えることができると共に、回収物の有効利用を阻害するシンゲナイト（Ｋ2Ｃａ（ＳＯ4）2）等の生成を抑制することができる。 In addition, in order to remove potassium and chlorine in the slurry in the solid-liquid separator, 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.
　さらに、また、ＣａＣｌ2は水に溶解するため、Ｃａ（ＯＨ）2に変化させなければ、後段で回収した工業塩に含まれることとなり、工業塩の純度を低下させる要因になるが、アルカリ剤との反応で水に溶解し難いＣａ（ＯＨ）2に変化させているため、工業塩の純度の低下を防止することもできる。 Furthermore, since CaCl 2 dissolves in water, if it is not changed to Ca (OH) 2 , it will be contained in the industrial salt recovered later, and this will cause a decrease in the purity of the industrial salt. since the varied hard Ca (OH) 2 dissolved in water by reaction with, it is also possible to prevent a reduction in the purity of the industrial salt.
　また、アルカリ剤の添加により、塩素バイパスダストに含まれる重金属のうち鉛（Ｐｂ）とセレン（Ｓｅ）が、ろ液側に多く含まれることなるため、後段で硫化剤等を用いて鉛を回収することができ、セレンは回収した工業塩に含まれることとなっても問題はないため、塩素バイパスダストから効率よく鉛及びセレンを除去することができる。 In addition, 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.
　上記塩素バイパス排ガスの処理装置において、前記脱硫塔から排出されたスラリーを固液分離する第２の固液分離装置と、該第２の固液分離装置で固液分離されたろ液を前記第２の溶解槽に供給する供給手段とを備えることができる。これによって、固液分離されたろ液を循環使用して有効利用することができると共に、ケーク側に石膏を回収することができる。 In the chlorine bypass exhaust gas treatment device, 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. Supply means for supplying to the dissolution tank. As a result, the filtrate separated from the solid and the liquid can be recycled and used effectively, and gypsum can be recovered on the cake side.
　上記塩素バイパス排ガスの処理装置において、前記第１の固液分離装置で固液分離されたろ液に硫化剤及びｐＨ調整剤を添加し、該ろ液に含まれる重金属を不溶化させる調整槽を備えることができる。これによって、鉛等を不溶化させて後段で効率よく回収することができる。 In the chlorine bypass exhaust gas treatment apparatus, 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.
　上記塩素バイパス排ガスの処理装置において、前記調整槽から排出されたろ液を固液分離する第３の固液分離装置を備えることができる。これによって、鉛等の重金属をケーク側に回収することができる。 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.
　上記塩素バイパス排ガスの処理装置において、前記第３の固液分離装置から排出されたろ液から塩を回収する塩回収装置を備えることができ、さらに、前記抽気ガスから回収した熱を前記塩回収装置における塩回収に利用するガスガスヒータを備えることができる。これにより、塩素バイパス排ガスの保有する熱を有効利用しながら塩を回収することができる。 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.
　前記ガスガスヒータは、前記抽気ガスを集塵する高温集塵機の排ガスから熱回収することができ、除塵した高温ガスから熱回収することで熱効率が向上する。 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.
　また、本発明は、塩素バイパス排ガスの処理方法であって、セメントキルンの窯尻から最下段サイクロンに至るまでのキルン排ガス流路より燃焼ガスの一部を冷却しながら抽気し、該抽気ガスから塩素バイパスダストを回収する塩素バイパス設備において、前記回収された塩素バイパスダストにアルカリ剤を添加しながらスラリー化した後、該スラリーを脱水し、得られたケークを再溶解させ、該ケークが再溶解したスラリーを該塩素バイパス設備の排ガスに接触させ、該排ガスの脱硫を行うことを特徴とする。本発明によれば、上記発明と同様に、塩素バイパスダストに含まれるカルシウム分を脱硫に有効に利用して塩素バイパス排ガスを処理することができ、スケールトラブルの原因となる石膏の溶解を最小限に抑えることができると共に、回収物の有効利用を阻害するシンゲナイト（Ｋ2Ｃａ（ＳＯ4）2）等の生成を抑制することができ、回収する工業塩の純度の低下を防止することもでき、塩素バイパスダストから効率よく鉛及びセレンを除去することもできる。 Further, 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. In 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. According to 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. In addition, it is possible to suppress the production of syngenite (K 2 Ca (SO 4 ) 2 ) that inhibits the effective use of the recovered material, and it is possible to prevent a decrease in the purity of the industrial salt to be recovered. Further, lead and selenium can be efficiently removed from the chlorine bypass dust.
　上記塩素バイパス排ガスの処理方法において、前記スラリーのｐＨを１３以上１４以下に調整することができ、このｐＨ領域で効率よく塩素バイパスダストに含まれるＣａＣｌ2及びＣａＣＯ3をＣａ（ＯＨ）2に変化させることができる。 In the chlorine bypass exhaust gas treatment method, 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.
　以上のように、本発明によれば、塩素バイパス排ガスを、セメント焼成系の熱損失を増加させることなく、セメント焼成系の安定運転を確保しながら、低コストで処理することができる。 As described above, according to the present invention, 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.
本発明にかかる塩素バイパス排ガスの処理装置の第１の実施形態を示す全体構成図である。BRIEF DESCRIPTION OF THE DRAWINGS It is a whole block diagram which shows 1st Embodiment of the processing apparatus of the chlorine bypass waste gas concerning this invention. 本発明にかかる塩素バイパス排ガスの処理装置の第２の実施形態を示す全体構成図である。It is a whole block diagram which shows 2nd Embodiment of the processing apparatus of the chlorine bypass waste gas concerning this invention. 従来の塩素バイパス設備を示す全体構成図である。It is a whole block diagram which shows the conventional chlorine bypass installation.
  次に、本発明を実施するための形態について図面を参照しながら説明する。 Next, embodiments for carrying out the present invention will be described with reference to the drawings.
　図１は、本発明にかかる塩素バイパス排ガスの処理装置の第１の実施形態を設けた塩素バイパス設備を示し、この塩素バイパス設備１は、セメントキルン２の窯尻から最下段サイクロン（不図示）に至るまでのキルン排ガス流路より、燃焼ガスの一部Ｇを冷却ファン４、５からの冷風で冷却しながら抽気するプローブ３と、プローブ３で抽気した抽気ガスＧ１に含まれるダストの粗粉Ｄ１を分離するサイクロン６と、サイクロン６から排出された微粉Ｄ２を含む抽気ガスＧ２を冷却する冷却器７と、冷却器７からの抽気ガスＧ３を集塵するバグフィルタ８と、バグフィルタ８からファン１０を介して供給された排ガスＧ４の脱硫処理を行う脱硫塔１１と、冷却器７及びバグフィルタ８から排出されたダストＤ５（Ｄ３＋Ｄ４）を貯留するダストタンク９と、ダストタンク９から排出されたダスト（塩素バイパスダスト）Ｄ６にアルカリ剤を添加しながらスラリー化する第１の溶解槽１２と、第１の溶解槽１２から排出されたスラリーＳ１を固液分離する第１の固液分離装置１３と、脱硫塔１１で発生したスラリーＳ３を固液分離する第２の固液分離装置１５と、第１の固液分離装置１３から排出されたケークＣ１を第２の固液分離装置１５からのろ液Ｌ２（循環水ＣＷ）に溶解させる第２の溶解槽１４と、第１の固液分離装置１３から排出されたろ液Ｌ１に硫化剤やｐＨ調整剤を添加する調整槽１６と、調整槽１６から排出されたろ液Ｌ３を固液分離する第３の固液分離装置１７等で構成される。プローブ３～ダストタンク９の構成については、２基の冷却ファン４、５で燃焼ガスＧを冷却する点を除き、従来の塩素バイパス設備と同様の構成であるため、詳細説明を省略する。 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). From the kiln exhaust gas flow path leading to the air, 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 adjustment tank 16 to which the agent is added, the third solid-liquid separation device 17 for solid-liquid separation of the filtrate L3 discharged from the adjustment tank 16, and the like. Since the configuration of the probe 3 to the dust tank 9 is the same as that of the conventional chlorine bypass equipment except that the combustion gas G is cooled by the two cooling fans 4 and 5, detailed description thereof is omitted.
　第１の溶解槽１２は、ダストタンク９からのダストＤ６を水（又は温水）を用いてスラリー化すると共に、ＮａＯＨ等のアルカリ剤を添加してダストＤ６に含まれるＣａＣｌ2及びＣａＣＯ3をＣａ（ＯＨ）2に変化させるために設けられる。 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 .
　第１の固液分離装置１３は、第１の溶解槽１２から排出されたスラリーＳ１を固液分離するために備えられる。固液分離されたケークＣ１は第２の溶解槽１４へ、ろ液Ｌ１は調整槽１６へ供給される。 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.
  第２の溶解槽１４は、第１の固液分離装置１３から排出されたケークＣ１を再溶解させるために備えられ、ケークＣ１を循環水ＣＷに溶解させたスラリーＳ２は、脱硫塔１１においてバグフィルタ８の排ガスＧ４の脱硫に利用される。 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.
　脱硫塔１１は、バグフィルタ８からファン１０を介して供給された排ガスＧ４を第２の溶解槽１４から供給されたスラリーＳ２を利用して脱硫するために備えられる。脱硫によって生じた二水石膏を含むスラリーＳ３は第２の固液分離装置１５へ、脱硫された排ガスＧ５は、セメントキルン２の排ガス系へ戻される。 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.
　第２の固液分離装置１５は、脱硫塔１１から供給されたスラリーＳ３を固液分離するために備えられ、固液分離されたろ液Ｌ２は、循環水ＣＷとして第２の溶解槽１４で再利用される。一方、固液分離されたケークＣ２側に二水石膏Ｇｙが回収される。 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.
　調整槽１６は、第１の固液分離装置１３から排出されたろ液Ｌ１にＮａＳＨ等の硫化剤やｐＨ調整剤を添加し、鉛等の重金属を不溶化させるために備えられる。ｐＨ調整剤として、ＮａＯＨ、Ｃａ（ＯＨ）2、ＣａＯ、Ｍｇ（ＯＨ）2、さらに硫酸等を用いることができる。 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. As the pH adjuster, NaOH, Ca (OH) 2 , CaO, Mg (OH) 2 , sulfuric acid or the like can be used.
　第３の固液分離装置１７は、調整槽１６から排出されたろ液Ｌ３を固液分離するために備えられ、固液分離されたろ液Ｌ４から塩回収装置によって工業塩を回収してもよく、排水処理することもできる。また、固液分離されたケークＣ３側に鉛等の重金属が回収される。 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.
　次に、上記構成を有する塩素バイパス設備１の動作について、図１を参照しながら説明する。 Next, the operation of the chlorine bypass facility 1 having the above configuration will be described with reference to FIG.
　セメントキルン２の窯尻から最下段サイクロンに至るまでのキルン排ガス流路からの燃焼ガスの一部Ｇをプローブ３によって抽気しながら、冷却ファン４、５からの冷風によって冷却する。これによって、塩素化合物の微結晶が生成される。この塩素化合物の微結晶は、抽気ガスＧ１に含まれるダストの微粉側に偏在しているため、サイクロン６で分級した粗粉Ｄ１をセメントキルン２に付設されたプレヒータ等にセメント原料として戻す。 While the part 3 of the combustion gas from the kiln exhaust gas flow path from the bottom of the kiln 2 of the cement kiln 2 to the lowermost cyclone is extracted by the probe 3, it is cooled by the cold air from the cooling fans 4 and 5. Thereby, microcrystals of the chlorine compound are generated. Since the fine crystals of the chlorine compound are unevenly distributed on the fine powder side of the dust contained in the extraction gas G1, the coarse powder D1 classified by the cyclone 6 is returned to the preheater or the like attached to the cement kiln 2 as a cement raw material.
　サイクロン６によって分離された微粉Ｄ２を含む抽気ガスＧ２を冷却器７に導入し、抽気ガスＧ２と媒体との熱交換を行う。熱交換によって冷却された抽気ガスＧ３をバグフィルタ８に導入し、バグフィルタ８において抽気ガスＧ３に含まれるダストＤ４を回収する。バグフィルタ８で回収したダストＤ４は、冷却器７から排出されたダストＤ３と共にダストＤ５としてダストタンク９に一旦貯留し、第１の溶解槽１２にダストＤ６として導入する。 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.
　第１の溶解槽１２に導入されたダストＤ６は、第１の溶解槽１２内において水（又は温水）及びＮａＯＨ等のアルカリ剤と混合されてスラリーＳ１が生成される。ここで、第１の溶解槽１２内のｐＨを１３．５±０．５に調整する。これにより、ダストＤ６に含まれるＣａＣｌ2及びＣａＣＯ3がアルカリ剤と反応してＣａ（ＯＨ）2が生成され、これらのカルシウム分を後段の脱硫塔１１における脱硫に有効に利用することができる。尚、アルカリ剤には、ＮａＯＨの他、ＫＯＨなどを用いることもできる。 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. Here, the pH in the first dissolution tank 12 is adjusted to 13.5 ± 0.5. As a result, 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. As the alkaline agent, KOH or the like can be used in addition to NaOH.
　また、ＣａＣｌ2は水に溶解するため、上記アルカリ剤と反応させてＣａ（ＯＨ）2に変化させなければ、後段の第３の固液分離装置１７のろ液Ｌ４に含まれ、回収した工業塩に含まれることとなる。その結果、工業塩の純度を低下させることとなるため、上記アルカリ剤との反応は、工業塩の純度の低下を防止するという効果も奏する。 In addition, since CaCl 2 is dissolved in water, it is contained in the recovered filtrate L4 of the third solid-liquid separation device 17 in the subsequent stage unless it is converted into Ca (OH) 2 by reacting with the alkali agent. It will be included in the salt. As a result, since the purity of the industrial salt is lowered, the reaction with the alkali agent also has an effect of preventing the purity of the industrial salt from being lowered.
　さらに、上記アルカリ剤の添加により、ダストＤ６に含まれる重金属のうち鉛（Ｐｂ）とセレン（Ｓｅ）が、ろ液Ｌ１とろ液Ｌ２に各々図１に示す割合で分離され、調整槽１６側に多く供給されるため、後段の調整槽１６及び第３の固液分離装置１７を介して鉛を効率よく回収することができる。尚、セレンは調整槽１６及び第３の固液分離装置１７によって回収されることは少ないが、回収した工業塩に含まれることとなっても問題はないため、ダストＤ６から効率よく除去することができる。一方、ケークＣ１に含まれるカドミウム、銅、亜鉛、鉛、セレン等の不溶金属及びフッ素化合物は、最終的に第２の固液分離装置１５において石膏Ｇｙと共に系外に排出される。 Furthermore, lead (Pb) and selenium (Se) among heavy metals contained in the dust D6 are separated into the filtrate L1 and the filtrate L2 in the ratio shown in FIG. Since a large amount is supplied, lead can be efficiently recovered through the adjustment tank 16 and the third solid-liquid separator 17 at the subsequent stage. Selenium is rarely recovered by the adjustment tank 16 and the third solid-liquid separation device 17, but there is no problem even if it is included in the recovered industrial salt, so it should be efficiently removed from the dust D6. Can do. On the other hand, insoluble metals such as cadmium, copper, zinc, lead, selenium and fluorine compounds contained in the cake C1 are finally discharged out of the system together with the gypsum Gy in the second solid-liquid separator 15.
　次に、第１の溶解槽１２から排出されたスラリーＳ１を第１の固液分離装置１３によって固液分離し、スラリーＳ１を固液分離しながら固液分離して得られるケークを水洗して塩素分を除去する。塩素分が除去されたケークＣ１を第２の溶解槽１４へ供給して再溶解させたスラリーＳ２を脱硫塔１１に供給して脱硫に利用する。尚、脱硫後の排ガスＧ５は、セメントキルン２の排ガス系へ導入する。 Next, 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.
　ここで、上記再溶解したスラリーＳ２中に存在するＣａ（ＯＨ）2が、脱硫塔１１でバグフィルタ８の排ガスＧ４に含まれるＳＯ2と反応して二水石膏（ＣａＳＯ4・２Ｈ2Ｏ）へと転換される。この際、第１の固液分離装置１３においてカリウム分や塩素分を除去したため、ケークＣ１を再溶解したスラリーＳ２の塩素含有率が低く、スケールトラブルの原因となる石膏の溶解を最小限に抑えることができると共に、シンゲナイト（Ｋ2Ｃａ（ＳＯ4）2）の生成を抑制することができる。尚、シンゲナイトがセメントに添加されると、セメント品質、特に強度に影響を及ぼすため生成を抑制しなければならない。 Here, 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.
　次に、第２の固液分離装置１５によって、脱硫塔１１から排出されたスラリーＳ３を固液分離してケークＣ２側に得られる二水石膏Ｇｙをセメントミルでセメントクリンカと共に粉砕してセメント製造に供することができる。一方、分離されたろ液Ｌ２を循環水ＣＷとして第２の溶解槽１４でのスラリーＳ２の生成に再利用することができる。 Next, 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. On the other hand, 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.
　一方、第１の固液分離装置１３によって固液分離されたろ液Ｌ１を調整槽１６に供給し、ろ液Ｌ１にＮａＳＨ等の硫化剤やｐＨ調整剤を添加し、鉛等の重金属を沈殿化させ、第３の固液分離装置１７で固液分離してケークＣ３側に重金属を回収する。尚、必要であれば、ろ液Ｌ３を第３の固液分離装置１７に供給する前にろ過助剤を添加する。また、第３の固液分離装置１７で固液分離されたろ液Ｌ４から工業塩を回収してもよく、ろ液Ｌ４を排水処理後に放流してもよい。工業塩を回収した場合には、上述のようにＣａＣｌ2をＣａ（ＯＨ）2に変化させたため、低カルシウム濃度でＫＣｌ含有率の高い工業塩を得ることができる。 On the other hand, 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.
　次に、本発明にかかる塩素バイパス排ガスの処理装置の第２の実施形態について、図２を参照しながら説明する。 Next, a second embodiment of the chlorine bypass exhaust gas treatment apparatus according to the present invention will be described with reference to FIG.
　この塩素バイパス設備３１は、塩素バイパス設備１の冷却器７及びバグフィルタ８に代えて高温集塵機３２を備え、高温集塵機３２の後段にガスガスヒータ３３を配置し、ガスガスヒータ３３で昇温された大気を塩回収に利用することを特徴とする。塩素バイパス設備３１の他の構成要素については、図１に示した塩素バイパス設備１と同様であるため、同一の参照番号を付してそれらについての説明を省略する。 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.
　高温集塵機３２は、例えば、セラミックフィルタを備え、９００℃程度までの耐熱性を有する耐熱型のバグフィルタや耐熱性を有する高温処理タイプの電気集塵機であって、サイクロン６から排出された微粉Ｄ２を含む抽気ガスＧ２を冷却せずに集塵し、集塵したダスト（塩素バイパスダスト）Ｄ３をダストタンク９に供給する。 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.
　ガスガスヒータ３３は、高温集塵機３２から排出された抽気ガスＧ３によって周囲から取り入れた空気Ａ１を加熱し、ガスガスヒータ３３で加熱された高温空気Ａ２を後段の塩回収に利用するために備えられる。また、空気Ａ２との熱交換により、脱硫塔１１で脱硫する排ガスＧ４の温度の調整が可能となり、固結の発生を抑制することができる。さらに、ガスガスヒータ３３で回収した熱を脱硫塔１１の排ガスＧ５の昇温に利用してもよい。 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.
　上記構成により、サイクロン６によって分離された微粉Ｄ２を含む抽気ガスＧ２を高温集塵機３２に導入し、高温集塵機３２において抽気ガスＧ２に含まれるダストＤ２を回収し、高温集塵機３２から排出されたダストＤ３は、ダストタンク９に一旦貯留し、第１の溶解槽１２にダストＤ４として導入する。また、周囲から取り入れた空気Ａ１及び高温集塵機３２の排ガスＧ３は、ガスガスヒータ３３に導入され、両者間で熱交換がなされた後、高温空気Ａ２は、塩回収に利用され、ガスガスヒータ３３から排出された排ガスＧ４は、脱硫塔１１に導入後脱硫される。その他のフローは塩素バイパス設備１の場合と同様である。 With the above configuration, 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. In addition, 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.
　以上のように、本実施の形態における塩素バイパス排ガスの処理装置は、第１の実施形態と同様の効果を奏すると共に、塩素バイパス排ガスの顕熱を塩回収に利用することで、塩回収のコストを低減することなどが可能となる。 As described above, the chlorine bypass exhaust gas treatment apparatus according to the present embodiment 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.
　また、上記実施の形態においては、溶解槽１２にダストＤ６を溶解させる場合について説明したが、カルシウム分が不足する場合には、サイクロン６で分離した粗粉Ｄ１を分取し、溶解槽１２や溶解槽１４に溶解させてカルシウム分を補うこともできる。 Moreover, in the said embodiment, although the case where the dust D6 was dissolved in the dissolution tank 12 was demonstrated, when calcium content is insufficient, the coarse powder D1 isolate | separated with the cyclone 6 is fractionated, and dissolution tank 12 or It can also be dissolved in the dissolution tank 14 to supplement the calcium content.
１　塩素バイパス設備
２　セメントキルン
３　プローブ
４、５　冷却ファン
６　サイクロン
７　冷却器
８　バグフィルタ
９　ダストタンク
１０　ファン
１１　脱硫塔
１２　第１の溶解槽
１３　第１の固液分離装置
１４　第２の溶解槽
１５　第２の固液分離装置
１６　調整槽
１７　第３の固液分離装置
３１　塩素バイパス設備
３２　高温集塵機
３３　ガスガスヒータ DESCRIPTION OF SYMBOLS 1 Chlorine bypass facility 2 Cement kiln 3 Probe 4, 5 Cooling fan 6 Cyclone 7 Cooler 8 Bag filter 9 Dust tank 10 Fan 11 Desulfurization tower 12 1st dissolution tank 13 1st solid-liquid separation apparatus 14 2nd dissolution tank 15 Second solid-liquid separator 16 Adjustment tank 17 Third solid-liquid separator 31 Chlorine bypass facility 32 High-temperature dust collector 33 Gas gas heater

Claims (9)

  1. 　セメントキルンの窯尻から最下段サイクロンに至るまでのキルン排ガス流路より燃焼ガスの一部を冷却しながら抽気し、該抽気ガスから塩素バイパスダストを回収する塩素バイパス設備に付設され、
    　前記回収された塩素バイパスダストにアルカリ剤を添加しながらスラリー化する第１の溶解槽と、
    　該第１の溶解槽で生成されたスラリーを固液分離する固液分離装置と、
    　該固液分離装置で生成されたケークを再溶解させる第２の溶解槽と、
    　前記第２の溶解槽で生成された再溶解後のスラリーを該塩素バイパス設備の排ガスに接触させ、該排ガスの脱硫を行う脱硫塔とを備えることを特徴とする塩素バイパス排ガスの処理装置。     Extracted while cooling a part of the combustion gas from the kiln exhaust gas flow path from the bottom of the kiln of the cement kiln to the bottom cyclone, and attached to a chlorine bypass facility for recovering chlorine bypass dust from the extracted gas,
    A first dissolution tank that is slurried while adding an alkali agent to the recovered chlorine bypass dust;
    A solid-liquid separation device for solid-liquid separation of the slurry produced in the first dissolution tank;
    A second dissolution tank for re-dissolving the cake produced by the solid-liquid separator;
    An apparatus for treating chlorine bypass exhaust gas, comprising: a desulfurization tower configured to contact the exhaust gas of the chlorine bypass facility with the redissolved slurry generated in the second dissolution tank and desulfurize the exhaust gas.
  2. 　前記脱硫塔から排出されたスラリーを固液分離する第２の固液分離装置と、該第２の固液分離装置で固液分離されたろ液を前記第２の溶解槽に供給する供給手段とを備えることを特徴とする請求項１に記載の塩素バイパス排ガスの処理装置。 A second solid-liquid separation device for solid-liquid separation of the slurry discharged from the desulfurization tower, and a supply means for supplying the filtrate separated by the second solid-liquid separation device to the second dissolution tank The chlorine bypass exhaust gas treatment device according to claim 1, comprising:
  3. 　前記第１の固液分離装置で固液分離されたろ液に硫化剤及びｐＨ調整剤を添加し、該ろ液に含まれる重金属を不溶化させる調整槽を備えることを特徴とする請求項１又は２に記載の塩素バイパス排ガスの処理装置。 3. A control tank for adding a sulfiding agent and a pH adjuster to the filtrate solid-liquid separated by the first solid-liquid separator and insolubilizing heavy metals contained in the filtrate is provided. An apparatus for treating chlorine bypass exhaust gas as described in 1.
  4. 　前記調整槽から排出されたろ液を固液分離する第３の固液分離装置を備えることを特徴とする請求項１、２又は３に記載の塩素バイパス排ガスの処理装置。 The chlorine bypass exhaust gas treatment device according to claim 1, 2 or 3, further comprising a third solid-liquid separation device for solid-liquid separation of the filtrate discharged from the adjustment tank.
  5. 　前記第３の固液分離装置から排出されたろ液から塩を回収する塩回収装置を備えることを特徴とする請求項４に記載の塩素バイパス排ガスの処理装置。 The chlorine bypass exhaust gas treatment device according to claim 4, further comprising a salt recovery device that recovers salt from the filtrate discharged from the third solid-liquid separation device.
  6. 　前記抽気ガスから回収した熱を前記塩回収装置における塩回収に利用するガスガスヒータを備えることを特徴とする請求項５に記載の塩素バイパス排ガスの処理装置。 The chlorine bypass exhaust gas treatment device according to claim 5, further comprising a gas gas heater that uses heat recovered from the extracted gas for salt recovery in the salt recovery device.
  7. 　前記ガスガスヒータは、前記抽気ガスを集塵する高温集塵機の排ガスから熱回収することを特徴とする請求項６に記載の塩素バイパス排ガスの処理装置。 The chlorine bypass exhaust gas treatment device according to claim 6, wherein the gas gas heater recovers heat from the exhaust gas of a high-temperature dust collector that collects the extracted gas.
  8. 　セメントキルンの窯尻から最下段サイクロンに至るまでのキルン排ガス流路より燃焼ガスの一部を冷却しながら抽気し、該抽気ガスから塩素バイパスダストを回収する塩素バイパス設備において、
    　前記回収された塩素バイパスダストにアルカリ剤を添加しながらスラリー化した後、該スラリーを脱水し、
    　得られたケークを再溶解させ、
    　該ケークが再溶解したスラリーを該塩素バイパス設備の排ガスに接触させ、該排ガスの脱硫を行うことを特徴とする塩素バイパス排ガスの処理方法。     In the chlorine bypass facility for extracting the chlorine bypass dust from the extracted gas while extracting a part of the combustion gas from the kiln exhaust gas passage from the kiln bottom of the cement kiln to the lowermost cyclone,
    After slurrying while adding an alkali agent to the recovered chlorine bypass dust, the slurry is dehydrated,
    Redissolve the resulting cake,
    A method for treating a chlorine bypass exhaust gas, wherein the slurry in which the cake is re-dissolved is brought into contact with the exhaust gas of the chlorine bypass facility to desulfurize the exhaust gas.
  9. 　前記スラリーのｐＨを１３以上１４以下に調整することを特徴とする請求項８に記載の塩素バイパス排ガスの処理方法。 9. The chlorine bypass exhaust gas treatment method according to claim 8, wherein the pH of the slurry is adjusted to 13 or more and 14 or less.
PCT/JP2012/051519 2011-03-09 2012-01-25 Device and method for processing chlorine bypass exhaust gas WO2012120933A1 (en)

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