JP2012101158A - Exhaust gas treating method and apparatus - Google Patents

Exhaust gas treating method and apparatus Download PDF

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JP2012101158A
JP2012101158A JP2010250578A JP2010250578A JP2012101158A JP 2012101158 A JP2012101158 A JP 2012101158A JP 2010250578 A JP2010250578 A JP 2010250578A JP 2010250578 A JP2010250578 A JP 2010250578A JP 2012101158 A JP2012101158 A JP 2012101158A
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exhaust gas
gas
heat exchanger
heating
heat
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JP5416679B2 (en
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Takuo Ueda
拓郎 上田
Atsushi Katagawa
篤 片川
Koji Muramoto
考司 村本
Jun Shimamura
潤 島村
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Mitsubishi Power Ltd
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Babcock Hitachi KK
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Priority to KR1020137014512A priority patent/KR20130116276A/en
Priority to BR112013010014A priority patent/BR112013010014A2/en
Priority to TW100140995A priority patent/TW201231147A/en
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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
    • 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
    • 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
    • B01D53/14—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 by absorption
    • 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
    • B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • 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
    • B01D2251/606—Carbonates
    • 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
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • 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
    • B01D2258/025—Other waste gases from metallurgy plants
    • 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
    • B01D53/343—Heat recovery
    • 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
    • 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
    • F23J2215/10—Nitrogen; 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 
    • 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 
    • F23J2219/00—Treatment devices
    • F23J2219/10—Catalytic reduction devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/40—Sorption with wet devices, e.g. scrubbers

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Biomedical Technology (AREA)
  • Health & Medical Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Treating Waste Gases (AREA)
  • Chimneys And Flues (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)

Abstract

PROBLEM TO BE SOLVED: To provide an exhaust gas treating method and apparatus by which desulfurization and denitrification in exhaust gas can be carried out even when the exhaust gas is the one discharged from a treatment gas producing apparatus other than burning apparatuses.SOLUTION: The exhaust gas discharged from a facility for sintering iron ore in an iron making process or the like is subjected to dust removal treatment and is subsequently heated by means of an exhaust gas heating burner 5, nitrogen oxide in the exhaust gas is removed by catalytic action, heat of the exhaust gas after removal of the nitrogen oxide is collected and is reused for heating for the nitrogen oxide removal from the exhaust gas by the catalytic action. Then sulfur oxide or the like in the exhaust gas of which the temperature has been decreased is removed from the exhaust gas using an absorption solution.

Description

本発明は排ガス処理装置と方法に係り、特に排ガス中のＮＯｘ、ＳＯｘ、煤塵及び、ペレットプラントなどで使用する燃料中に含まれる成分や物質を低減する排煙処理設備に関する。   The present invention relates to an exhaust gas treatment apparatus and method, and more particularly, to a flue gas treatment facility for reducing components and substances contained in fuel used in NOx, SOx, soot and pellet plant in exhaust gas.

製鉄所で使用する鉄鉱石ペレットを製造するペレットプラントなどから排出される排ガスは、化石燃料などを使用する燃焼装置からの排ガスに比べて温度が低い。これらの排ガスには燃焼装置からの排ガスと同様に窒素酸化物（ＮＯｘ）や硫黄酸化物（ＳＯｘ）が含まれるので、大気汚染防止のためにＮＯｘやＳＯｘを除去する必要がある。   The temperature of exhaust gas discharged from a pellet plant that manufactures iron ore pellets used at steelworks is lower than that of exhaust gas from combustion devices that use fossil fuels. Since these exhaust gases contain nitrogen oxides (NOx) and sulfur oxides (SOx) like the exhaust gases from the combustion apparatus, it is necessary to remove NOx and SOx to prevent air pollution.

一般的な排ガス処理システムの系統を図７に示す。この排ガス処理システムでは、ペレットプラント１などから排出される排ガスは電気集塵機２で排ガス中の煤塵を除去した後、湿式排煙脱硫装置７に導入され、排煙脱硫装置７内に噴霧される脱硫剤スラリと気液接触して、排ガス中のＳＯｘが取り除かれる。排煙脱硫装置７で処理された排ガスは、その温度が飽和温度まで下がっているため、ファン３によりガスガス熱交換器４に送られ、さらに排ガス加熱バーナ５により、脱硝装置６で必要な温度にまで加熱される。また、電気集塵機２を経由した排ガスが排煙脱硫装置７を経由しないで、直接ファン３によりガス熱交換機４に送られることもある。加熱された排ガスは脱硝装置６に導入されて排ガス中のＮＯｘが脱硝触媒と接触することにより取り除かれ、再びガスガス熱交換器４を経て、煙突８より排出される。   A general exhaust gas treatment system system is shown in FIG. In this exhaust gas treatment system, the exhaust gas discharged from the pellet plant 1 or the like is introduced into the wet flue gas desulfurization device 7 after the dust in the exhaust gas is removed by the electric dust collector 2 and desulfurized to be sprayed into the exhaust gas desulfurization device 7. The SOx in the exhaust gas is removed by gas-liquid contact with the agent slurry. Since the temperature of the exhaust gas treated by the flue gas desulfurization device 7 is lowered to the saturation temperature, the exhaust gas is sent to the gas gas heat exchanger 4 by the fan 3, and further to the temperature required by the denitration device 6 by the exhaust gas heating burner 5. Until heated. Further, the exhaust gas passing through the electric dust collector 2 may be sent directly to the gas heat exchanger 4 by the fan 3 without passing through the flue gas desulfurization device 7. The heated exhaust gas is introduced into the denitration device 6, and NOx in the exhaust gas is removed by contacting with the denitration catalyst, and is again discharged from the chimney 8 through the gas gas heat exchanger 4.

特開２０００−３００９６１号公報JP 2000-300961 A

図７に示す湿式排煙脱硫装置７を通過した排ガスは、飽和温度まで冷却されるため、脱硝装置６内の脱硝触媒上で酸性硫安の生成を防ぐために必要な温度にまで、ガスガス熱交換器４と排ガス加熱バーナ５の組み合わせで再加熱する必要があり、多くの燃料を使用する問題点がある。
排ガス加熱バーナ５は、排煙脱硫装置７の後流側の排ガス流路に設置されるため、排ガス加熱バーナ５の燃焼により生成したＳＯｘは除去されず排出される。排出規制の問題上、排ガス加熱バーナ５の燃焼で生成するＳＯｘを低減するため、硫黄分含有量の低い高品位の燃料を使用する必要がある。
本発明の課題は、燃焼装置以外の処理ガスが発生する装置から排出する排ガスであっても、該排ガス中の脱硫と脱硝を行うための排ガス処理方法と装置を提供することである。 Since the exhaust gas that has passed through the wet flue gas desulfurization device 7 shown in FIG. 7 is cooled to the saturation temperature, the gas gas heat exchanger is brought to a temperature necessary for preventing the formation of acidic ammonium sulfate on the denitration catalyst in the denitration device 6. 4 and the exhaust gas heating burner 5 need to be reheated, and there is a problem of using a lot of fuel.
Since the exhaust gas heating burner 5 is installed in the exhaust gas flow path on the downstream side of the flue gas desulfurization device 7, the SOx generated by the combustion of the exhaust gas heating burner 5 is discharged without being removed. In order to reduce SOx produced by the combustion of the exhaust gas heating burner 5, it is necessary to use a high-grade fuel with a low sulfur content because of emission control problems.
An object of the present invention is to provide an exhaust gas treatment method and apparatus for performing desulfurization and denitration in exhaust gas, even if the exhaust gas is exhausted from an apparatus that generates process gas other than the combustion apparatus.

上記した問題点を解決するには、湿式排煙脱硫装置７を脱硝装置６の後流に設置することで解決できる。
請求項１に記載の発明は、製鉄工程で鉄鉱石を焼結する設備またはボイラから排出される排ガスを除塵処理した後、排ガス加熱バーナ（５）で加熱して、脱硝触媒を用いて排ガス中の窒素酸化物を除去し、窒素酸化物を除去した後の排ガスの熱を熱交換により回収して前記脱硝触媒を用いて排ガス中の窒素酸化物を除去するための排ガスの加熱に利用し、次いで前記熱交換により温度低下した排ガス中の硫黄酸化物及びその他の成分に起因する物質を石灰石または石灰を含むスラリよりなる吸収液を用いて吸収・除去することを特徴とする排ガス処理方法である。 In order to solve the above-mentioned problems, the wet flue gas desulfurization device 7 can be solved by installing it in the downstream of the denitration device 6.
According to the first aspect of the present invention, the exhaust gas discharged from the equipment or boiler that sinters iron ore in the iron making process is dedusted, and then heated by the exhaust gas heating burner (5), and the denitration catalyst is used in the exhaust gas. The nitrogen oxide is removed, and the heat of the exhaust gas after removing the nitrogen oxide is recovered by heat exchange and used for heating the exhaust gas to remove the nitrogen oxide in the exhaust gas using the denitration catalyst, Next, the exhaust gas treatment method is characterized by absorbing and removing substances caused by sulfur oxides and other components in the exhaust gas whose temperature has been lowered by the heat exchange, using an absorption liquid comprising a slurry containing limestone or lime. .

請求項２に記載の発明は、前記脱硝触媒を用いて排ガス中の窒素酸化物を除去した後の排ガスの熱を、前記脱硝触媒を用いて排ガス中の窒素酸化物の除去に再び利用した後、さらに熱交換により回収して、前記排ガス加熱バーナ（５）の燃焼用空気（１１）の加熱に利用することを特徴とする請求項１記載の排ガス処理方法である。   In the invention according to claim 2, after the heat of the exhaust gas after removing the nitrogen oxide in the exhaust gas using the denitration catalyst is used again for the removal of the nitrogen oxide in the exhaust gas using the denitration catalyst Furthermore, it collect | recovers by heat exchange, It uses for the heating of the combustion air (11) of the said exhaust gas heating burner (5), The exhaust gas processing method of Claim 1 characterized by the above-mentioned.

請求項３に記載の発明は、前記熱交換により回収して前記排ガス加熱バーナ（５）の燃焼用空気（１１）の加熱に利用して、温度の低下した排ガスから、前記石灰石または石灰を含むスラリよりなる吸収液を用いて硫黄酸化物及びその他の成分に起因する物質を吸収・除去することを特徴とする請求項２記載の排ガス処理方法である。   The invention according to claim 3 includes the limestone or the lime from the exhaust gas whose temperature has been reduced, recovered by the heat exchange and used for heating the combustion air (11) of the exhaust gas heating burner (5). 3. The exhaust gas treatment method according to claim 2, wherein a substance resulting from sulfur oxide and other components is absorbed and removed using an absorbing liquid made of slurry.

請求項４に記載の発明は、製鉄工程で鉄鉱石を焼結する設備またはボイラから排出される排ガスが流れる排ガス流路に、排ガスの除塵処理をする集塵器（２）と、該集塵器（２）の出口排ガスを加熱する排ガス加熱バーナ（５）と、該排ガス加熱バーナ（５）で加熱された排ガス中の窒素酸化物を除去する脱硝触媒を充填した脱硝装置（６）と、該脱硝装置（６）の出口排ガスから熱回収して脱硝装置（６）の入口排ガスを加熱するガスガス熱交換器（４）と、該ガスガス熱交換器（４）の出口排ガスを導入して排ガス中の硫黄酸化物及びその他の成分に起因する物質を石灰石または石灰を含むスラリよりなる吸収液を用いて吸収・除去する湿式排煙脱硫装置（７）を配置したことを特徴とする排ガス処理装置である。   The invention according to claim 4 is a dust collector (2) for performing dust removal treatment of exhaust gas in an exhaust gas flow path in which exhaust gas discharged from a facility or boiler for sintering iron ore in an iron making process, and the dust collection An exhaust gas heating burner (5) for heating the outlet exhaust gas of the vessel (2), and a denitration device (6) filled with a denitration catalyst for removing nitrogen oxides in the exhaust gas heated by the exhaust gas heating burner (5); A gas gas heat exchanger (4) for recovering heat from the exhaust gas at the outlet of the denitration device (6) to heat the exhaust gas at the inlet of the denitration device (6), and an exhaust gas by introducing the exhaust gas at the outlet of the gas gas heat exchanger (4) Exhaust gas treatment device characterized in that a wet flue gas desulfurization device (7) that absorbs and removes substances resulting from sulfur oxides and other components in the slurry using an absorption liquid made of slurry containing limestone or lime is provided. It is.

請求項５に記載の発明は、前記ガスガス熱交換器（４）出口の排ガス流路に第２のガスガス熱回収器（９）を設け、該第２のガスガス熱交換器（９）と排ガス加熱バーナ（５）に供給する燃焼用空気（１１）の導入路に設けたガスガス熱再熱器（１０）を熱媒体流路（１３）で接続したことを特徴とする請求項４記載の排ガス処理装置である。   According to the fifth aspect of the present invention, a second gas gas heat recovery device (9) is provided in the exhaust gas flow path at the outlet of the gas gas heat exchanger (4), and the second gas gas heat exchanger (9) and the exhaust gas heating are provided. The exhaust gas treatment according to claim 4, characterized in that the gas gas heat reheater (10) provided in the introduction path of the combustion air (11) supplied to the burner (5) is connected by the heat medium flow path (13). Device.

請求項６に記載の発明は、第２のガスガス熱交換器（９）の出口側の温度が低下した排ガス流路を湿式排煙脱硫装置（７）に接続したことを特徴とする請求項５記載の排ガス処理装置である。   The invention described in claim 6 is characterized in that the exhaust gas flow path whose temperature on the outlet side of the second gas gas heat exchanger (9) is lowered is connected to the wet flue gas desulfurization device (7). It is an exhaust-gas-treatment apparatus of description.

本発明において、湿式排煙脱硫装置７を脱硝装置６の後流側の排ガス流路に設置することで、ガスガス熱交換器４の入口の排ガス温度低下を防ぐことが可能となる。これにより、ガスガス熱交換器４の仕様を小さくできる上、排ガス加熱バーナ５の燃料使用量を低減することが可能となる。
また排ガス加熱バーナ５に硫黄分を多量に含む重油など幅広い種類の燃料を使用できる上、ガスガス熱交換器４の入口排ガスが乾燥排ガスとなるため、ガスガス熱交換器４の材料選定が容易になる。 In the present invention, by installing the wet flue gas desulfurization device 7 in the exhaust gas flow path on the downstream side of the denitration device 6, it is possible to prevent a decrease in the exhaust gas temperature at the inlet of the gas gas heat exchanger 4. Thereby, the specification of the gas gas heat exchanger 4 can be reduced, and the amount of fuel used by the exhaust gas heating burner 5 can be reduced.
In addition, a wide variety of fuels such as heavy oil containing a large amount of sulfur can be used for the exhaust gas heating burner 5, and the exhaust gas at the inlet of the gas gas heat exchanger 4 becomes a dry exhaust gas, which makes it easy to select the material for the gas gas heat exchanger 4. .

本発明となる排ガス処理装置の系統を示した図である。It is the figure which showed the system | strain of the exhaust gas processing apparatus used as this invention. 本発明（図２（ａ））及び従来技術（図２（ｂ））の排ガス処理装置の温度バランスを示した図である。It is the figure which showed the temperature balance of the waste gas processing apparatus of this invention (FIG.2 (a)) and a prior art (FIG.2 (b)). 本発明（図３（ａ））と従来技術（図３（ｂ））からなる排ガス処理装置のＳＯｘ濃度バランスを示した図である。It is the figure which showed the SOx density | concentration balance of the waste gas processing apparatus which consists of this invention (FIG. 3 (a)) and a prior art (FIG.3 (b)). 脱硫性能と排煙脱硫装置の吸収液循環液量の関係を示した図である。It is the figure which showed the relationship between desulfurization performance and the amount of absorption liquid circulating fluids of a flue gas desulfurization apparatus. 図５（ａ）と図５（ｂ）は共に本発明となる排ガス処理装置にＧＧＨ熱回収器−再加熱器を追加した図である。5 (a) and 5 (b) are diagrams in which a GGH heat recovery device-reheater is added to the exhaust gas treatment apparatus according to the present invention. 排煙脱硫装置の入口排ガス温度と蒸発水量の関係を示した図である。It is the figure which showed the relationship between the inlet exhaust gas temperature of a flue gas desulfurization apparatus, and the amount of evaporated water. 従来の排ガス処理装置の系統を示した図である。It is the figure which showed the system | strain of the conventional waste gas processing apparatus.

本発明の実施例を図面と共に説明する。   Embodiments of the present invention will be described with reference to the drawings.

本発明による排ガス処理系統を図１に示す。製鉄所で使用する鉄鉱石ペレットを製造するペレットプラント１からの排ガス流路において、ガスガス熱交換器４を周知の石灰石スラリなどを用いる湿式排煙脱硫装置７の前流側に設置し、湿式排煙脱硫装置７を周知の脱硝触媒を配置した脱硝装置６の後流側に設置する。なお、図１などで説明する装置で図７に示す装置と同一機能を奏する装置には、同一番号を付して、その説明を省略する場合がある。   An exhaust gas treatment system according to the present invention is shown in FIG. In the exhaust gas flow path from the pellet plant 1 that manufactures the iron ore pellets used in the steelworks, the gas gas heat exchanger 4 is installed on the upstream side of the wet flue gas desulfurization device 7 using a known limestone slurry, etc. The smoke desulfurization device 7 is installed on the downstream side of the denitration device 6 in which a known denitration catalyst is arranged. In addition, the apparatus which demonstrates the same function as the apparatus shown in FIG. 7 by the apparatus demonstrated in FIG. 1 etc. may attach | subject the same number, and may abbreviate | omit the description.

図２にガスガス熱交換器４周りの温度バランスの例を示す。図２（ｂ）は従来の排ガス処理系統で、排煙脱硫装置７の後流側の排ガス流路に脱硝装置６を設置する場合の温度バランスであるが、排煙脱硫装置７を出た排ガスの温度は、硫黄酸化物と窒素酸化物が飽和した飽和ガスでありガスガス熱交換器４の手前で約５０℃にまで下がる。
この排ガスを、脱硝処理するために必要な温度である約３５０℃まで加熱する必要があるため、その加熱にはガスガス熱交換器４と排ガス加熱バーナ５の組み合わせで行うことができるが、温度上昇幅が大きいため、ガスガス熱交換器４の仕様が大きくなったり、排ガス加熱バーナ５の燃料を多量に使用したりするため経済的でない。また、排ガスが硫黄酸化物と窒素酸化物で飽和しているため、ガスガス熱交換器４の材質に耐腐食性の材質を採用する必要があり経済的でない。 FIG. 2 shows an example of the temperature balance around the gas gas heat exchanger 4. FIG. 2B shows a conventional exhaust gas treatment system, which shows the temperature balance when the denitration device 6 is installed in the exhaust gas flow path on the downstream side of the exhaust gas desulfurization device 7. Is a saturated gas saturated with sulfur oxides and nitrogen oxides, and decreases to about 50 ° C. before the gas gas heat exchanger 4.
Since it is necessary to heat this exhaust gas to about 350 ° C., which is a temperature necessary for denitration treatment, the heating can be performed by a combination of the gas gas heat exchanger 4 and the exhaust gas heating burner 5, but the temperature rises. Since the width is large, the specifications of the gas gas heat exchanger 4 are increased, and a large amount of fuel from the exhaust gas heating burner 5 is used, which is not economical. Further, since the exhaust gas is saturated with sulfur oxide and nitrogen oxide, it is necessary to employ a corrosion-resistant material as the material of the gas gas heat exchanger 4, which is not economical.

図２（ａ）に示す本発明の実施例の装置では、排煙脱硫装置７を脱硝装置６の後流側の排ガス流路に設置することにより、脱硝装置６の手前のガスガス熱交換器４の入口の排ガス温度は１５０℃であり、ガスガス熱交換器４の仕様を小さくできる上、排ガス加熱バーナ５で使用する燃料の使用量を低減することが可能となる。
さらに、従来の排ガス処理装置では排煙脱硫装置７を脱硝装置６の手前の排ガス流路に設置していたため、硫黄酸化物と窒素酸化物で飽和した排ガスがガスガス熱交換器４に導入される。そのため、ガスガス熱交換器４において耐腐食性を考慮した材料選定が必要であった。 In the apparatus of the embodiment of the present invention shown in FIG. 2 (a), by installing the flue gas desulfurization device 7 in the exhaust gas flow path on the downstream side of the denitration device 6, the gas gas heat exchanger 4 in front of the denitration device 6 is provided. The exhaust gas temperature at the inlet of the exhaust gas is 150 ° C., so that the specification of the gas gas heat exchanger 4 can be reduced and the amount of fuel used in the exhaust gas heating burner 5 can be reduced.
Further, in the conventional exhaust gas treatment device, the flue gas desulfurization device 7 is installed in the exhaust gas flow channel before the denitration device 6, so that the exhaust gas saturated with sulfur oxide and nitrogen oxide is introduced into the gas gas heat exchanger 4. . Therefore, it is necessary to select a material in consideration of corrosion resistance in the gas gas heat exchanger 4.

本発明の装置では、排煙脱硫装置７を脱硝装置６の後流側の排ガス流路に設置することにより、ガスガス熱交換器４には乾燥した排ガスが導入されるためガスガス熱交換器４の材料選定を容易にすることが可能となる。
また、本実施例の装置では排煙脱硫装置７を脱硝装置６の後流側の排ガス流路に設置することにより、排ガス加熱バーナ５で生成するＳＯｘも除去することが可能となる。これにより硫黄分を含む燃料など幅広い燃料を排ガス加熱バーナ５で使用することが可能となる。 In the apparatus of the present invention, by installing the flue gas desulfurization device 7 in the exhaust gas flow path on the downstream side of the denitration device 6, dry exhaust gas is introduced into the gas gas heat exchanger 4, so that the gas gas heat exchanger 4 Material selection can be facilitated.
Further, in the apparatus of this embodiment, by installing the flue gas desulfurization apparatus 7 in the exhaust gas flow path on the downstream side of the denitration apparatus 6, it is possible to remove SOx generated by the exhaust gas heating burner 5. This makes it possible to use a wide range of fuel such as fuel containing sulfur in the exhaust gas heating burner 5.

図３に排煙処理システムのＳＯｘ濃度のバランスを示す。図３（ｂ）は、従来の湿式排煙脱硫装置７を脱硝装置６の上流に設置した場合のＳＯｘ濃度バランスの例である。排煙脱硫装置７の後流側の排ガス流路に排ガス加熱バーナ５が設置されているため、硫黄分を含む重油を排ガス加熱バーナ５の燃料に使用した場合、排ガス加熱バーナ５の燃料の燃焼で発生した約１２００ｐｐｍの高濃度のＳＯｘは処理されること無く、煙突８へと導かれる。煙突８の入口でのＳＯｘ濃度を５０ｐｐｍとした場合、排ガス加熱バーナ５からの排出される排ガス中のＳＯｘを考慮して排煙脱硫装置７の必要性能を決定する必要があり、本例では、排煙脱硫装置７において約９８％の脱硫性能が必要となる。   FIG. 3 shows the SOx concentration balance of the flue gas treatment system. FIG. 3B is an example of the SOx concentration balance when the conventional wet flue gas desulfurization device 7 is installed upstream of the denitration device 6. Since the exhaust gas heating burner 5 is installed in the exhaust gas flow path on the downstream side of the flue gas desulfurization device 7, when heavy oil containing sulfur is used as the fuel of the exhaust gas heating burner 5, the combustion of the fuel of the exhaust gas heating burner 5 The high-concentration SOx of about 1200 ppm generated in step 1 is led to the chimney 8 without being processed. When the SOx concentration at the inlet of the chimney 8 is 50 ppm, it is necessary to determine the required performance of the flue gas desulfurization device 7 in consideration of SOx in the exhaust gas discharged from the exhaust gas heating burner 5, In the flue gas desulfurization apparatus 7, a desulfurization performance of about 98% is required.

図３（ａ）に示す本実施例の装置では、排煙脱硫装置７を脱硝装置６の後流側の排ガス流路に設置することで排ガス加熱バーナ５で発生したＳＯｘも除去することが可能となり、煙突８の入口でのＳＯｘ濃度を５０ｐｐｍとした場合、排煙脱硫装置７において必要な脱硫性能は約９５％となる。本実施例では必要脱硫性能を約３％低減することが可能となる。   In the apparatus of the present embodiment shown in FIG. 3A, it is possible to remove SOx generated in the exhaust gas heating burner 5 by installing the flue gas desulfurization apparatus 7 in the exhaust gas flow path on the downstream side of the denitration apparatus 6. Thus, when the SOx concentration at the inlet of the chimney 8 is 50 ppm, the desulfurization performance required in the flue gas desulfurization apparatus 7 is about 95%. In this embodiment, the required desulfurization performance can be reduced by about 3%.

図４に必要脱硫性能と排煙脱硫装置７での石灰石スラリなどからなる吸収液循環液量（排煙脱硫装置７内に導入された排ガスに対して前記吸収液を噴霧して、気液接触による脱硫反応をさせ、落下した吸収液を脱硫装置下部の貯留タンク（図示せず）に貯めた後、何度も排ガスに対して噴霧するために循環させる）の関係を示すが、必要脱硫性能が９８％から９５％へ３％低減することにより吸収液循環液量を約２０％低減することが可能となり、電力消費量の低減や吸収液循環ポンプの台数低減が可能となる。   FIG. 4 shows the required desulfurization performance and the amount of the circulating liquid of the absorbing liquid composed of limestone slurry in the flue gas desulfurization apparatus 7 (the above-mentioned absorbing liquid is sprayed on the exhaust gas introduced into the flue gas desulfurization apparatus 7 to contact the gas and liquid The desulfurization reaction is carried out, and the fallen absorption liquid is stored in a storage tank (not shown) at the bottom of the desulfurization unit and then circulated to spray the exhaust gas repeatedly. By reducing 3% from 98% to 95%, it becomes possible to reduce the amount of the circulating liquid of the absorbing liquid by about 20%, and it becomes possible to reduce the power consumption and the number of the absorbing liquid circulating pumps.

本発明の他の実施例を図５に示す。図５に示す排煙処理システムは、図１に示す排煙処理システムに第２のガスガス熱交換器９を脱硝装置６の後流側であって脱硫装置７の前流側の排ガス流路に配置した例である。
図５（ａ）に示す例では、脱硝装置６の後流側の排ガス流路に配置する第２のガスガス熱交換器９の出口の排ガスは２００℃程度であり、この排ガスが湿式排煙脱硫装置７に導入され、飽和温度まで冷却されて煙突８から排出される。本実施例では、排煙脱硫装置７の手前の排ガス流路に第２のガスガス熱回収器９を設置し、ガスガス熱回収器４で回収した熱をガスガス再加熱器１０に熱媒体ライン１３から供給し、排ガス加熱バーナ５の燃焼用空気１１の予熱に使用することで、これまで使用されていなかった熱を有効に利用することが可能となる。 Another embodiment of the present invention is shown in FIG. The smoke emission treatment system shown in FIG. 5 has a second gas gas heat exchanger 9 in the exhaust gas flow path on the downstream side of the denitration device 6 and on the upstream side of the desulfurization device 7 in the smoke emission treatment system shown in FIG. This is an example of arrangement.
In the example shown in FIG. 5A, the exhaust gas at the outlet of the second gas gas heat exchanger 9 disposed in the exhaust gas flow path on the downstream side of the denitration device 6 is about 200 ° C., and this exhaust gas is wet flue gas desulfurization. It is introduced into the device 7, cooled to the saturation temperature and discharged from the chimney 8. In the present embodiment, the second gas gas heat recovery device 9 is installed in the exhaust gas flow channel before the flue gas desulfurization device 7, and the heat recovered by the gas gas heat recovery device 4 is transferred from the heat medium line 13 to the gas gas reheater 10. By supplying and using it for preheating the combustion air 11 of the exhaust gas heating burner 5, it becomes possible to effectively use heat that has not been used so far.

図５（ｂ）に示すように、ガスガス熱回収器４の他に排ガス加熱用空気エアヒータ１２を用いて、排ガス加熱バーナ５の燃焼用空気１１の予熱に使用することも可能である。
また、排ガスは排煙脱硫装置７で冷却される際に多量の蒸発水が煙突８から排出されることとなる。図６に排煙脱硫装置７の入口温度と蒸発水量の関係を示す。排ガス温度が２００℃で排煙脱硫装置７に導入された場合は約１５０ｔ／ｈの水が蒸発するのに対して、排ガス温度が１００℃の場合は約５０ｔ／ｈの水が蒸発することとなる。 As shown in FIG. 5B, it is possible to use the exhaust gas heating air air heater 12 in addition to the gas gas heat recovery device 4 to preheat the combustion air 11 of the exhaust gas heating burner 5.
Further, when the exhaust gas is cooled by the flue gas desulfurization device 7, a large amount of evaporated water is discharged from the chimney 8. FIG. 6 shows the relationship between the inlet temperature of the flue gas desulfurization device 7 and the amount of evaporated water. When the exhaust gas temperature is 200 ° C. and introduced into the flue gas desulfurization device 7, about 150 t / h of water evaporates, whereas when the exhaust gas temperature is 100 ° C., about 50 t / h of water evaporates; Become.

本実施例では、ガスガス熱回収器４を湿式排煙脱硫装置７の手前に設置することで、排煙脱硫装置７に導入される排ガス温度を下げることにより蒸発水量を低減することができ、排煙処理システムでの水の消費量を低減することが可能となる。   In this embodiment, by installing the gas gas heat recovery device 4 in front of the wet flue gas desulfurization device 7, the amount of evaporated water can be reduced by lowering the exhaust gas temperature introduced into the flue gas desulfurization device 7. It is possible to reduce water consumption in the smoke treatment system.

ペレット製造プラントなどから排出する温度の低い排ガス中のＮＯｘ、ＳＯｘを効率よく処理できる設備として本発明は利用可能性が高い。   The present invention has high applicability as equipment capable of efficiently treating NOx and SOx in exhaust gas having a low temperature discharged from a pellet manufacturing plant or the like.

１ ペレットプラント ２ 電気集塵機
３ ファン ４ ガスガス熱交換器
５ 排ガス加熱バーナ ６ 脱硝装置
７ 湿式排煙脱硫装置 ８ 煙突
９ 第２のガスガス熱交換器
１０ 再加熱器 １１ 燃焼用空気
１２ 排ガス加熱用空気エアヒータ
１３ 熱媒体ライン DESCRIPTION OF SYMBOLS 1 Pellet plant 2 Electric dust collector 3 Fan 4 Gas gas heat exchanger 5 Exhaust gas heating burner 6 Denitration device 7 Wet flue gas desulfurization device 8 Chimney 9 Second gas gas heat exchanger
10 Reheater 11 Combustion air
12 Air Air Heater for Exhaust Gas Heating 13 Heat Medium Line

本発明は排ガス処理装置と方法に係り、特に排ガス中のＮＯｘ、ＳＯｘ、煤塵及びペレットプラントなどで使用する燃料中に含まれる成分や物質を低減する排煙処理設備に関する。 The present invention relates to an exhaust gas processing apparatus and method, in particular NOx in the exhaust gas, SOx, relates flue gas treatment facility to reduce the components and substances contained in the fuel used in the soot及beauty pellet plant.

一般的な排ガス処理システムの系統を図７に示す。この排ガス処理システムでは、ペレットプラント１などから排出される排ガスは電気集塵機２で排ガス中の煤塵を除去した後、湿式排煙脱硫装置７に導入され、排煙脱硫装置７内に噴霧される脱硫剤スラリと気液接触して、排ガス中のＳＯｘが取り除かれる。排煙脱硫装置７で処理された排ガスは、その温度が飽和温度まで下がっているため、ファン３によりガスガス熱交換器４に送られ、さらに排ガス加熱バーナ５により、脱硝装置６で必要な温度にまで加熱される。また、電気集塵機２を経由した排ガスが排煙脱硫装置７を経由しないで、直接ファン３によりガスガス熱交換器４に送られることもある。加熱された排ガスは脱硝装置６に導入されて排ガス中のＮＯｘが脱硝触媒と接触することにより取り除かれ、再びガスガス熱交換器４を経て、煙突８より排出される。 A general exhaust gas treatment system system is shown in FIG. In this exhaust gas treatment system, the exhaust gas discharged from the pellet plant 1 or the like is introduced into the wet flue gas desulfurization device 7 after the dust in the exhaust gas is removed by the electric dust collector 2 and desulfurized to be sprayed into the exhaust gas desulfurization device 7. The SOx in the exhaust gas is removed by gas-liquid contact with the agent slurry. Since the temperature of the exhaust gas treated by the flue gas desulfurization device 7 is lowered to the saturation temperature, the exhaust gas is sent to the gas gas heat exchanger 4 by the fan 3, and further to the temperature required by the denitration device 6 by the exhaust gas heating burner 5. Until heated. Further, the exhaust gas passing through the electrostatic precipitator 2 without passing through the flue gas desulfurization apparatus 7, also be sent directly by the fan 3 to the gas-gas heat exchanger 4. The heated exhaust gas is introduced into the denitration device 6, and NOx in the exhaust gas is removed by contacting with the denitration catalyst, and is again discharged from the chimney 8 through the gas gas heat exchanger 4.

請求項３に記載の発明は、前記熱交換により回収して前記排ガス加熱バーナ（５）の燃焼用空気（１１）の加熱に利用して、温度の低下した排ガスを、前記石灰石または石灰を含むスラリよりなる吸収液と接触させて、該排ガスから硫黄酸化物及びその他の成分に起因する物質を吸収・除去することを特徴とする請求項２記載の排ガス処理方法である。 Invention of Claim 3 collect | recovers by the said heat exchange, and utilizes it for the heating of the combustion air (11) of the said waste gas heating burner (5), The waste gas which temperature fell contains the said limestone or lime 3. The exhaust gas treatment method according to claim 2, wherein substances caused by sulfur oxides and other components are absorbed and removed from the exhaust gas by contacting with an absorption liquid made of slurry.

請求項５に記載の発明は、前記ガスガス熱交換器（４）出口の排ガス流路に第２のガスガス熱交換器（９）を設け、該第２のガスガス熱交換器（９）と排ガス加熱バーナ（５）に供給する燃焼用空気（１１）の導入路に設けたガスガス熱再熱器（１０）を熱媒体流路（１３）で接続したことを特徴とする請求項４記載の排ガス処理装置である。 According to the fifth aspect of the present invention, a second gas gas heat exchanger (9) is provided in the exhaust gas passage at the outlet of the gas gas heat exchanger (4), and the second gas gas heat exchanger (9) and the exhaust gas heating are provided. The exhaust gas treatment according to claim 4, characterized in that the gas gas heat reheater (10) provided in the introduction path of the combustion air (11) supplied to the burner (5) is connected by the heat medium flow path (13). Device.

請求項６に記載の発明は、第２のガスガス熱交換器（９）の出口側の温度が低下した排ガス流路を湿式排煙脱硫装置（７）に接続したことを特徴とする請求項５記載の排ガス処理装置である。
請求項７に記載の発明は、前記ガスガス熱交換器（４）出口の排ガス流路に排ガス加熱バーナ（５）の燃焼用空気（１１）を加熱するエアヒータ（１２）を設け、該エアヒータ（１２）で加熱された空気を排ガス加熱バーナ（５）に供給する燃焼用空気流路を設けたことを特徴とする請求項４記載の排ガス処理装置である。 The invention described in claim 6 is characterized in that the exhaust gas flow path whose temperature on the outlet side of the second gas gas heat exchanger (9) is lowered is connected to the wet flue gas desulfurization device (7). It is an exhaust gas processing apparatus of description.
According to the seventh aspect of the present invention, an air heater (12) for heating combustion air (11) of the exhaust gas heating burner (5) is provided in the exhaust gas flow path at the outlet of the gas gas heat exchanger (4), and the air heater (12 The exhaust gas treatment device according to claim 4, further comprising a combustion air flow path for supplying the air heated in step) to the exhaust gas heating burner (5).

請求項１、４記載の発明によれば、湿式排煙脱硫装置７を脱硝装置６の後流側の排ガス流路に設置することで、ガスガス熱交換器４の入口の排ガス温度低下を防ぐことが可能となる。これにより、ガスガス熱交換器４の仕様を小さくできる上、排ガス加熱バーナ５の燃料使用量を低減することが可能となる。
また排ガス加熱バーナ５に硫黄分を多量に含む重油など幅広い種類の燃料を使用できる上、ガスガス熱交換器４の入口排ガスが乾燥排ガスとなるため、ガスガス熱交換器４の材料選定が容易になる。
請求項２、５、７記載の発明によれば、脱硝触媒を用いて排ガス中の窒素酸化物の除去に使用した後の排ガスの熱を、再び脱硝触媒の加熱のために熱交換して利用した後、排ガス加熱バーナ５の燃焼用空気１１の加熱に利用することで、これまで使用されていなかった熱を有効に利用することができる。
請求項３、６記載の発明によれば、排煙脱硫装置７を脱硝装置６の後流側の排ガス流路に設置することで排ガス加熱バーナ５で発生したＳＯｘも除去することが可能となり、煙突８の入口でのＳＯｘ濃度を５０ｐｐｍとした場合、排煙脱硫装置７において必要な脱硫性能は約９５％となり、必要脱硫性能を約３％低減することが可能となる。 According to the first and fourth aspects of the present invention, the wet flue gas desulfurization device 7 is installed in the exhaust gas passage on the downstream side of the denitration device 6, thereby preventing the exhaust gas temperature from decreasing at the inlet of the gas gas heat exchanger 4. Is possible. Thereby, the specification of the gas gas heat exchanger 4 can be reduced, and the amount of fuel used by the exhaust gas heating burner 5 can be reduced.
In addition, a wide variety of fuels such as heavy oil containing a large amount of sulfur can be used for the exhaust gas heating burner 5, and the exhaust gas at the inlet of the gas gas heat exchanger 4 becomes a dry exhaust gas, which makes it easy to select the material for the gas gas heat exchanger 4. .
According to the inventions of claims 2, 5 and 7, the heat of the exhaust gas after being used for removing nitrogen oxides in the exhaust gas using the denitration catalyst is again used for heat exchange for heating the denitration catalyst. After that, the heat that has not been used can be used effectively by using it for heating the combustion air 11 of the exhaust gas heating burner 5.
According to the inventions of claims 3 and 6, it is possible to remove SOx generated in the exhaust gas heating burner 5 by installing the flue gas desulfurization device 7 in the exhaust gas passage on the downstream side of the denitration device 6, When the SOx concentration at the inlet of the chimney 8 is 50 ppm, the required desulfurization performance in the flue gas desulfurization apparatus 7 is about 95%, and the required desulfurization performance can be reduced by about 3%.

図５（ａ）に示す例では、脱硝装置６の後流側の排ガス流路に配置する第２のガスガス熱交換器９の出口の排ガスは２００℃程度であり、この排ガスが湿式排煙脱硫装置７に導入され、飽和温度まで冷却されて煙突８から排出される。本実施例では、排煙脱硫装置７の手前の排ガス流路に第２のガスガス熱交換器９を設置し、ガスガス熱交換器４で回収した熱をガスガス再加熱器１０に熱媒体ライン１３から供給し、排ガス加熱バーナ５の燃焼用空気１１の予熱に使用することで、これまで使用されていなかった熱を有効に利用することが可能となる。 In the example shown in FIG. 5A, the exhaust gas at the outlet of the second gas gas heat exchanger 9 disposed in the exhaust gas flow path on the downstream side of the denitration device 6 is about 200 ° C., and this exhaust gas is wet flue gas desulfurization. It is introduced into the device 7, cooled to the saturation temperature and discharged from the chimney 8. In the present embodiment, the second gas gas heat exchanger 9 is installed in the exhaust gas flow channel before the flue gas desulfurization device 7, and the heat recovered by the gas gas heat exchanger 4 is transferred from the heat medium line 13 to the gas gas reheater 10. By supplying and using it for preheating the combustion air 11 of the exhaust gas heating burner 5, it becomes possible to effectively use heat that has not been used so far.

図５（ｂ）に示すように、ガスガス熱交換器４の他に排ガス加熱用空気エアヒータ１２を用いて、排ガス加熱バーナ５の燃焼用空気１１の予熱に使用することも可能である。
また、排ガスは排煙脱硫装置７で冷却される際に多量の蒸発水が煙突８から排出されることとなる。図６に排煙脱硫装置７の入口温度と蒸発水量の関係を示す。排ガス温度が２００℃で排煙脱硫装置７に導入された場合は約１５０ｔ／ｈの水が蒸発するのに対して、排ガス温度が１００℃の場合は約５０ｔ／ｈの水が蒸発することとなる。 As shown in FIG. 5 (b), it is possible to use the exhaust gas heating air air heater 12 in addition to the gas gas heat exchanger 4 to preheat the combustion air 11 of the exhaust gas heating burner 5.
Further, when the exhaust gas is cooled by the flue gas desulfurization device 7, a large amount of evaporated water is discharged from the chimney 8. FIG. 6 shows the relationship between the inlet temperature of the flue gas desulfurization device 7 and the amount of evaporated water. When the exhaust gas temperature is 200 ° C. and introduced into the flue gas desulfurization device 7, about 150 t / h of water evaporates, whereas when the exhaust gas temperature is 100 ° C., about 50 t / h of water evaporates; Become.

本実施例では、ガスガス熱交換器４を湿式排煙脱硫装置７の手前に設置することで、排煙脱硫装置７に導入される排ガス温度を下げることにより蒸発水量を低減することができ、排煙処理システムでの水の消費量を低減することが可能となる。 In this embodiment, by installing the gas gas heat exchanger 4 in front of the wet flue gas desulfurization device 7, the amount of evaporated water can be reduced by lowering the exhaust gas temperature introduced into the flue gas desulfurization device 7. It is possible to reduce water consumption in the smoke treatment system.

Claims (6)

製鉄工程で鉄鉱石を焼結する設備またはボイラから排出される排ガスを除塵処理した後、排ガス加熱バーナ（５）で加熱して、脱硝触媒を用いて排ガス中の窒素酸化物を除去し、窒素酸化物を除去した後の排ガスの熱を熱交換により回収して前記脱硝触媒を用いて排ガス中の窒素酸化物を除去するための排ガスの加熱に利用し、次いで前記熱交換により温度低下した排ガス中の硫黄酸化物及びその他の成分に起因する物質を石灰石または石灰を含むスラリよりなる吸収液を用いて吸収・除去することを特徴とする排ガス処理方法。   After dust removal from exhaust gas discharged from equipment or boiler that sinters iron ore in the iron making process, it is heated with an exhaust gas heating burner (5) to remove nitrogen oxides in the exhaust gas using a denitration catalyst, and nitrogen The heat of the exhaust gas after removing the oxide is recovered by heat exchange and used for heating the exhaust gas to remove nitrogen oxides in the exhaust gas using the denitration catalyst, and then the exhaust gas whose temperature has decreased by the heat exchange An exhaust gas treatment method characterized by absorbing and removing substances caused by sulfur oxides and other components therein using an absorption liquid made of slurry containing limestone or lime. 前記脱硝触媒を用いて排ガス中の窒素酸化物を除去した後の排ガスの熱を前記脱硝触媒を用いて排ガス中の窒素酸化物の除去に再び利用した後、さらに熱交換により回収して前記排ガス加熱バーナ（５）の燃焼用空気（１１）の加熱に利用することを特徴とする請求項１記載の排ガス処理方法。   The heat of the exhaust gas after removing the nitrogen oxides in the exhaust gas using the denitration catalyst is reused for the removal of the nitrogen oxides in the exhaust gas using the denitration catalyst, and further recovered by heat exchange to recover the exhaust gas. 2. The exhaust gas treatment method according to claim 1, wherein the exhaust gas treatment method is used for heating the combustion air (11) of the heating burner (5). 前記熱交換により回収して前記排ガス加熱バーナ（５）の燃焼用空気（１１）の加熱に利用して、温度の低下した排ガスから、前記石灰石または石灰を含むスラリよりなる吸収液を用いて硫黄酸化物及びその他の成分に起因する物質を吸収・除去することを特徴とする請求項２記載の排ガス処理方法。   Sulfur using an absorbing liquid made of the limestone or lime-containing slurry from the exhaust gas whose temperature has decreased is recovered by the heat exchange and used for heating the combustion air (11) of the exhaust gas heating burner (5). The exhaust gas treatment method according to claim 2, wherein substances originating from oxides and other components are absorbed and removed. 製鉄工程で鉄鉱石を焼結する設備またはボイラから排出される排ガスが流れる排ガス流路に、排ガスの除塵処理をする集塵器（２）と、該集塵器（２）の出口排ガスを加熱する排ガス加熱バーナ（５）と、該排ガス加熱バーナ（５）で加熱された排ガス中の窒素酸化物を除去する脱硝触媒を充填した脱硝装置（６）と、該脱硝装置（６）の出口排ガスから熱回収して脱硝装置（６）の入口排ガスを加熱するガスガス熱交換器（４）と、該ガスガス熱交換器（４）の出口排ガスを導入して排ガス中の硫黄酸化物及びその他の成分に起因する物質を石灰石または石灰を含むスラリよりなる吸収液を用いて吸収・除去する湿式排煙脱硫装置（７）を配置したことを特徴とする排ガス処理装置。   Dust collector (2) for dust removal treatment of exhaust gas and heating exhaust gas at the outlet of the dust collector (2) to the exhaust gas flow path through which exhaust gas discharged from boilers or boilers that sinter iron ore in the iron making process Exhaust gas heating burner (5), a denitration device (6) filled with a denitration catalyst for removing nitrogen oxides in the exhaust gas heated by the exhaust gas heating burner (5), and an exhaust gas discharged from the denitration device (6) Gas gas heat exchanger (4) for recovering heat from the exhaust gas and heating the exhaust gas at the inlet of the denitration device (6), and introducing the exhaust gas at the outlet of the gas gas heat exchanger (4) to introduce sulfur oxides and other components in the exhaust gas An exhaust gas treatment apparatus comprising a wet flue gas desulfurization apparatus (7) that absorbs and removes substances caused by limestone using an absorption liquid made of limestone or a slurry containing lime. 前記ガスガス熱交換器（４）出口の排ガス流路に第２のガスガス熱回収器（９）を設け、該第２のガスガス熱交換器（９）と排ガス加熱バーナ（５）に供給する燃焼用空気（１１）の導入路に設けたガスガス熱再熱器（１０）を熱媒体流路（１３）で接続したことを特徴とする請求項４記載の排ガス処理装置。   A second gas gas heat recovery device (9) is provided in the exhaust gas flow path at the outlet of the gas gas heat exchanger (4), and is supplied to the second gas gas heat exchanger (9) and the exhaust gas heating burner (5). The exhaust gas treatment device according to claim 4, characterized in that a gas gas heat reheater (10) provided in the introduction path of air (11) is connected by a heat medium flow path (13). 第２のガスガス熱交換器（９）の出口側の温度が低下した排ガス流路を湿式排煙脱硫装置（７）に接続したことを特徴とする請求項５記載の排ガス処理装置。   6. The exhaust gas treatment device according to claim 5, wherein the exhaust gas flow path whose temperature on the outlet side of the second gas gas heat exchanger (9) has decreased is connected to the wet flue gas desulfurization device (7).
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