JP3423517B2 - Exhaust gas treatment method and device - Google Patents
Exhaust gas treatment method and deviceInfo
- Publication number
- JP3423517B2 JP3423517B2 JP35321495A JP35321495A JP3423517B2 JP 3423517 B2 JP3423517 B2 JP 3423517B2 JP 35321495 A JP35321495 A JP 35321495A JP 35321495 A JP35321495 A JP 35321495A JP 3423517 B2 JP3423517 B2 JP 3423517B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- exhaust gas
- dust
- heat recovery
- heater
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 238000000034 method Methods 0.000 title claims description 33
- 239000007789 gas Substances 0.000 claims description 159
- 239000000428 dust Substances 0.000 claims description 80
- 238000011084 recovery Methods 0.000 claims description 40
- 238000006477 desulfuration reaction Methods 0.000 claims description 24
- 230000023556 desulfurization Effects 0.000 claims description 23
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 20
- 239000003546 flue gas Substances 0.000 claims description 20
- 239000004071 soot Substances 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 239000003795 chemical substances by application Substances 0.000 claims description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 12
- 238000002485 combustion reaction Methods 0.000 claims description 11
- 239000002253 acid Substances 0.000 claims description 10
- 239000010440 gypsum Substances 0.000 claims description 9
- 229910052602 gypsum Inorganic materials 0.000 claims description 9
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 8
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 8
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 8
- 239000003245 coal Substances 0.000 claims description 8
- 239000004571 lime Substances 0.000 claims description 8
- 229920003002 synthetic resin Polymers 0.000 claims description 8
- 239000000057 synthetic resin Substances 0.000 claims description 8
- 239000004809 Teflon Substances 0.000 claims description 7
- 229920006362 Teflon® Polymers 0.000 claims description 7
- 239000010881 fly ash Substances 0.000 claims description 7
- 239000000571 coke Substances 0.000 claims description 6
- 238000003303 reheating Methods 0.000 claims description 6
- 235000019738 Limestone Nutrition 0.000 claims description 5
- 230000000903 blocking effect Effects 0.000 claims description 5
- 239000006028 limestone Substances 0.000 claims description 5
- 239000000779 smoke Substances 0.000 claims description 5
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 4
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 4
- 239000000920 calcium hydroxide Substances 0.000 claims description 4
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 4
- 235000012255 calcium oxide Nutrition 0.000 claims description 4
- 239000000292 calcium oxide Substances 0.000 claims description 4
- 238000004140 cleaning Methods 0.000 claims description 4
- 230000029142 excretion Effects 0.000 claims 1
- 230000007797 corrosion Effects 0.000 description 15
- 238000005260 corrosion Methods 0.000 description 15
- 239000004744 fabric Substances 0.000 description 11
- 239000000126 substance Substances 0.000 description 11
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 10
- 229910052753 mercury Inorganic materials 0.000 description 10
- 238000010586 diagram Methods 0.000 description 6
- 239000012717 electrostatic precipitator Substances 0.000 description 6
- 238000005406 washing Methods 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- 150000002013 dioxins Chemical class 0.000 description 5
- 229910000831 Steel Inorganic materials 0.000 description 4
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 4
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 4
- 235000011130 ammonium sulphate Nutrition 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005192 partition Methods 0.000 description 4
- 239000010959 steel Substances 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 239000011248 coating agent Substances 0.000 description 3
- 230000006698 induction Effects 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000011001 backwashing Methods 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000012719 wet electrostatic precipitator Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 101000606506 Homo sapiens Receptor-type tyrosine-protein phosphatase eta Proteins 0.000 description 1
- 102100039808 Receptor-type tyrosine-protein phosphatase eta Human genes 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000007429 general method Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
Landscapes
- Chimneys And Flues (AREA)
- Treating Waste Gases (AREA)
- Filtering Of Dispersed Particles In Gases (AREA)
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、石炭焚燃焼装置か
ら排出される燃焼排ガスを効率よく、かつ、経済的に処
理することができ、さらには排ガス中の水銀、ダイオキ
シンなどの有害物質を同時に除去することができる方法
及び装置に関するものである。TECHNICAL FIELD The present invention is capable of efficiently and economically treating combustion exhaust gas discharged from a coal-burning combustion device, and is capable of simultaneously treating harmful substances such as mercury and dioxins in the exhaust gas. It relates to a method and a device that can be removed.
【０００２】[0002]
【従来の技術】石炭を燃料とする火力発電所（石炭火
力）からの排煙に対しても、重油火力からの排煙並の低
い煤塵排出濃度が要求されている。この要求を達成する
ためには、単に集塵機の性能を強化するだけでは設備が
大きくなり過ぎることや腐食問題など経済的にも技術的
にも問題があり、排煙処理システム全体で除塵性能を改
善することが必要不可欠である。また、石炭に含まれる
水銀などの重金属の化合物をはじめとする有害物質及び
排ガス中のダイオキシンについても規制される傾向にあ
り、対策が急がれている。2. Description of the Related Art For smoke emitted from a coal-fired thermal power plant (coal-fired power), it is required to have a low soot emission concentration comparable to that emitted from heavy oil-fired power. In order to achieve this requirement, there are economic and technical problems such as equipment becoming too large and corrosion problems by simply enhancing the performance of the dust collector, and improving the dust removal performance of the entire flue gas treatment system. Is essential. Further, harmful substances such as compounds of heavy metals such as mercury contained in coal and dioxin in exhaust gas tend to be regulated, and countermeasures are urgently needed.
【０００３】すなわち、石炭燃焼排ガスには水銀、ダイ
オキシンなどの有害物質が含まれており、今後はこれら
についても排出規制が行われる傾向にある。これまでの
電気集塵機による方法では、水銀などの有害物質は殆ど
除去できない。また、脱硫装置の後流にバグフィルター
を設置することにより、水銀などの有害物質除去の問題
は解決されるが、設備構成が複雑になると同時に、系内
圧力損失の増加によりブロワの所用動力が大きくなり経
済的でない。In other words, coal combustion exhaust gas contains harmful substances such as mercury and dioxins, and in the future, emission regulations will also be applied to these substances. Most of the harmful substances such as mercury cannot be removed by the conventional electrostatic precipitator method. Also, by installing a bag filter in the downstream of the desulfurizer, the problem of removing harmful substances such as mercury can be solved, but at the same time the equipment configuration becomes complicated and the power loss of the blower increases the required power of the system. It becomes big and not economical.
【０００４】従来から、例えば特開平３−７０９０７号
公報に示されるように、石炭焚ボイラの排ガスを空気予
熱器及び熱回収器（例えばノンリーク式ガス・ガスヒー
タの熱回収部）で８０〜１１０℃に冷却した後、乾式電
気集塵機でダスト濃度を１００mg／Nm3 以下に低減さ
せ、さらに脱硫装置に導いてＳＯｘを低減させた後、再
加熱器（例えばノンリーク式のガス・ガスヒータの再加
熱部）に導いて、排ガスを加熱した後、煙突から排出す
るボイラ排ガスの処理方法が知られている。Conventionally, as disclosed in, for example, Japanese Patent Application Laid-Open No. 3-70907, the exhaust gas of a coal-fired boiler is heated at 80 to 110 ° C. in an air preheater and a heat recovery device (for example, a heat recovery section of a non-leak type gas / gas heater). After cooling to 0, the dust concentration is reduced to 100 mg / Nm 3 or less with a dry type electrostatic precipitator, and then it is led to a desulfurization device to reduce SOx, and then a reheater (for example, a reheating unit of a non-leak type gas / gas heater). There is known a method for treating boiler exhaust gas discharged from a chimney after heating the exhaust gas.
【０００５】また、従来の一般的な石炭焚排ガスの処理
方法として、図９に示すように、石炭焚燃焼装置、例え
ば石炭焚ボイラ１０からの排ガスを脱硝装置１２に導入
して脱硝処理した後、空気予熱器（ＧＡＨ）１４に導入
し、ついで乾式電気集塵機１６（以下、ＤＥＰというこ
ともある。）に導入して集塵した後、集塵された排ガス
を媒体循環式のガス・ガスヒータ（ＧＧＨ）１８の熱回
収器２０に導入して冷却した後、脱塵塔２２に導入し水
をスプレーして脱塵し、ついで、脱硫装置２４に導入し
て脱硫した後、媒体循環式のガス・ガスヒータ（ＧＧ
Ｈ）１８の再加熱器２６に導入し再加熱して煙突２８へ
導く方法が知られている。なお、媒体循環式のガス・ガ
スヒータの代わりにヒートパイプが用いられることも知
られている。Further, as a conventional general method for treating coal-burning exhaust gas, as shown in FIG. 9, after introducing the exhaust gas from a coal-burning combustor, for example, a coal-burning boiler 10 to a denitration device 12, denitration treatment is performed. , The air preheater (GAH) 14, and then the dry type electrostatic precipitator 16 (hereinafter, also referred to as DEP) to collect dust, and the collected exhaust gas is a medium circulation type gas / gas heater ( GGH) 18 is introduced into a heat recovery device 20 and cooled, and then introduced into a dedusting tower 22 for spraying water to remove dust, and then introduced into a desulfurization device 24 for desulfurization, followed by a medium circulation type gas.・ Gas heater (GG
It is known that H) 18 is introduced into the reheater 26, reheated, and led to the chimney 28. It is also known that a heat pipe is used instead of the medium circulation type gas / gas heater.
【０００６】図９に示す方式において、煤塵濃度を低下
させるには、電気集塵機（ＤＥＰ）１６の性能を上げる
方法が最も簡単であるが、この方法では次の欠点があ
る。
（１） 単なる性能向上では、炭種によってはＤＥＰの
集塵面積は過大になり（一般的な炭種の場合の１．５〜
２倍）、経済性に劣るばかりでなく、大きな敷地面積を
必要とする。
（２） ＤＥＰ１６の後流に通常設置されている媒体循
環式ガス・ガスヒータ１８の熱回収器２０において、排
ガス中の煤塵濃度が下がることにより酸の中和能力が低
下し、酸露点以下の部分で腐食が発生する。
なお、排ガス中の煤塵は、アルカリ成分を含んでいるた
め、排ガスの冷却によって凝縮する酸（硫酸）を中和
し、装置の腐食を防止する働きがあるため、通常は、１
００mg／Nm3 程度の煤塵を残すことが行われている。し
かし、多量の煤塵が脱硫装置に入ると、石膏の品質を低
下させることになるため、除塵塔を設置し、さらに、煤
塵の排出規制を守るためにＷＥＰを設置する方式が採用
されている。In the method shown in FIG. 9, the method of improving the performance of the electrostatic precipitator (DEP) 16 is the simplest to reduce the dust concentration, but this method has the following drawbacks. (1) With merely improving the performance, the dust collection area of DEP becomes too large depending on the type of coal (1.5 ~
It is not only economically inferior, but also requires a large site area. (2) In the heat recovery unit 20 of the medium circulation type gas / gas heater 18 which is usually installed in the downstream of the DEP 16, the neutralization ability of the acid is lowered due to the decrease of the dust concentration in the exhaust gas, and the temperature is below the acid dew point. Corrosion occurs. Since the dust in the exhaust gas contains an alkaline component, it has the function of neutralizing the acid (sulfuric acid) condensed by cooling the exhaust gas and preventing the corrosion of the device.
It is practiced to leave about 00 mg / Nm 3 of dust. However, if a large amount of soot dust enters the desulfurization device, the quality of gypsum will be deteriorated. Therefore, a method of installing a dust removal tower and further installing WEP to comply with the emission control of soot dust is adopted.
【０００７】図９に示す方式では、このような問題点が
あるため、ＤＥＰの出口濃度を下げずに図１０に示すよ
うに、脱硫装置２４の出口に湿式電気集塵機３０（以
下、ＷＥＰという。）を設置し、煤塵の低濃度化を図る
方式が実用化されている。図１０の方式は、安定して排
ガス中の煤塵濃度を低く押さえる運転が可能であるが、
経済性に劣る欠点がある。図１０の方式に変わるものと
して、図１１に示すように、ガス・ガスヒータ１８の熱
回収器２０をＤＥＰ１６の前流に設置する方式が提案さ
れている（前述の特開平３−７０９０７号公報参照）。
図１１の方式は、つぎのような優れた点を有している。
（１） ＤＥＰ１６の出口の排ガス温度が８０〜１１０
℃と低く、煤塵の電気抵抗値も低くなるので、ＤＥＰ１
６での集塵性能が向上する。
（２） ＤＥＰ１６の出口の煤塵濃度が低くなっても、
ガス・ガスヒータの熱回収器２０はＤＥＰの上流にある
ので、酸が煤塵により中和されて熱回収器２０の腐食の
懸念はない。
（３） ＤＥＰ１６の集塵性能が上がり、ＤＥＰ出口の
煤塵濃度が下がるので、脱硫装置２４への煤塵の混入量
が少なくなり、除塵塔（脱塵塔）がなくても副生石膏品
質は所定の品質が確保できる。
（４） また、ＷＥＰを設置しなくとも、煤塵を低濃度
（例えば、５mg／Nm3 以下）とすることができる。Since the system shown in FIG. 9 has such a problem, the wet electrostatic precipitator 30 (hereinafter referred to as WEP) is provided at the outlet of the desulfurization device 24 as shown in FIG. 10 without lowering the concentration of the DEP outlet. ) Is installed to reduce the concentration of soot and dust. The system of FIG. 10 is capable of stably operating to keep the dust concentration in exhaust gas low,
It has the disadvantage of being less economical. As an alternative to the method of FIG. 10, there is proposed a method of installing the heat recovery unit 20 of the gas / gas heater 18 in the upstream of the DEP 16 as shown in FIG. 11 (refer to the above-mentioned JP-A-3-70907). ).
The method of FIG. 11 has the following excellent points. (1) The exhaust gas temperature at the outlet of DEP16 is 80 to 110.
Since it is as low as ℃, and the electric resistance value of dust is also low, DEP1
The dust collection performance in No. 6 is improved. (2) Even if the dust concentration at the outlet of DEP16 becomes low,
Since the heat recovery unit 20 of the gas / gas heater is located upstream of the DEP, there is no concern about corrosion of the heat recovery unit 20 due to neutralization of acid by soot dust. (3) Since the dust collection performance of DEP16 is improved and the concentration of soot dust at the DEP outlet is reduced, the amount of soot dust mixed into the desulfurization device 24 is reduced, and the by-product gypsum quality is the same even if there is no dust removal tower (dust removal tower). Quality can be secured. (4) Further, it is possible to reduce the concentration of soot dust (for example, 5 mg / Nm 3 or less) without installing WEP.
【０００８】しかし、図１１に示す方式は、つぎのよう
な欠点を有している。
（ａ） ＤＥＰ１６の腐食、煤塵付着対策が必要
排ガス温度が低くなると、一般的には捕集煤塵の流動性
は悪化する。従って、電気集塵機１６内の集塵極や、放
電極、ホッパー等に煤塵が付着又は固着するので、その
対策が必要となる（保温強化、エアーレーション、放電
極等の構造の変更等が必要）。
（ｂ） ボイラ誘引ファン（ＩＤＦ）の腐食対策が必要
ＩＤＦはインペラーの磨耗防止の観点から、ＤＥＰの後
流に設置されるが、本方式でのＤＥＰ以降では、温度が
低く煤塵濃度も低いため、ＤＥＰを通過したＳＯ3 又は
硫酸ヒュームのＩＤＦへの飛来による腐食が懸念され、
一部耐食性材料の使用等による対処が必要であり、コス
ト高になる。
（ｃ） ガス・ガスヒータの熱回収器２０の長期安定運
転対策が必要
煤塵濃度がこれ迄に比べて２桁程高くなるので（１０g
〜２０g ／m N ）、煤塵による熱回収器２０の閉塞防止
対策に十分なる配慮が必要である。一般には、閉塞防止
対策として鋼球散布方式が採用されるが、高濃度の煤塵
になると、熱回収器２０の伝熱管表面に多くの煤塵が付
着するため、鋼球の落下による衝撃力が緩和され除去効
果が低減する。付着煤塵の除去が充分に行なわれない
と、伝熱効率が低下すると同時に圧力損失の増加を引き
起こし、ファン動力が増加する。However, the method shown in FIG. 11 has the following drawbacks. (A) Corrosion of DEP16 and measures against dust adhesion are required. When the exhaust gas temperature becomes low, the fluidity of collected dust is generally deteriorated. Therefore, soot dust adheres to or adheres to the dust collecting electrode in the electrostatic precipitator 16, the discharge electrode, the hopper, etc., and countermeasures for it are necessary (reinforcement of heat retention, aeration, structure change of discharge electrode, etc. are required). . (B) Corrosion measures for boiler induction fan (IDF) are required. IDF is installed in the downstream of DEP from the viewpoint of wear prevention of impeller, but since DEP in this method, temperature is low and soot concentration is low. , Corrosion due to SO 3 or fumes passing through DEP flying into IDF,
It is necessary to deal with the use of some corrosion-resistant materials, etc., resulting in high cost. (C) Measures for long-term stable operation of the heat recovery unit 20 of the gas / gas heater are required. Since the dust concentration is about two orders of magnitude higher than before (10 g
~ 20 g / m N), sufficient consideration is required for measures to prevent the heat recovery device 20 from being blocked by soot and dust. Generally, a steel ball spraying method is adopted as a measure to prevent clogging, but when high-concentration soot dust is generated, a large amount of soot dust adheres to the surface of the heat transfer tube of the heat recovery device 20, so the impact force due to the falling of the steel balls is mitigated. The removal effect is reduced. If the adhered dust is not sufficiently removed, the heat transfer efficiency is reduced and at the same time, the pressure loss is increased and the fan power is increased.
【０００９】[0009]
【発明が解決しようとする課題】火力発電所の環境対策
設備は、発電出力が大きくなるほど２系列で構成される
ことが多い。これは製造限界に起因することもあるが、
トラブル時に片系列運転が可能なように配慮しているこ
とにもよるものである。図１１に示す方式を２系列で構
成する場合は、図１２に示すようになる。３２は誘引フ
ァン、３４はブースタファンである。図１２に示す方式
では、次の問題点がある。
（ａ） 脱硫装置片系運転
環境対策設備の中でトラブルによる片系運転を行う可能
性の高いのは、カルシウムに起因するスケーリングによ
り圧力損失増加の懸念のある脱硫装置２４である。図１
２の方式により脱硫片系列運転を行う場合、ガス・ガス
ヒータの熱回収器２０側は２系列運転、再加熱器２６側
は１系列運転とならざるを得ず（１）停止系列の再加熱
器になんらかの対応策が必要、（２）運転側の再加熱後
の排ガス温度が低い（熱交換量が約半分）等の問題があ
る。
（ｂ） 全系片系列運転
脱硫片系運転では上記の問題があるので、脱硝を含めた
全系を片系列運転とすることも考えられるが、この場合
には次の問題がある。すなわち、処理する排ガス量は計
画量なるも、負荷は低負荷のため温度が低くなる。これ
は触媒を使用する脱硝では、脱硝性能が低下することと
なり、このような運転を最初から計画する場合は、触媒
量を予め多くしておく必要があり、コストが嵩むことに
なる。The environment-friendly equipment of a thermal power plant is often constructed of two series as the power generation output increases. This may be due to manufacturing limits,
This is also due to the fact that consideration is given to enabling single-line operation in the event of trouble. When the system shown in FIG. 11 is configured by two systems, it becomes as shown in FIG. Reference numeral 32 is an attracting fan, and 34 is a booster fan. The method shown in FIG. 12 has the following problems. (A) Desulfurization device One of the one-sided operating environment countermeasure facilities that is likely to perform one-sided operation due to a trouble is the desulfurization device 24 in which pressure loss may increase due to scaling due to calcium. Figure 1
When the desulfurization piece series operation is performed by the method of No. 2, the heat recovery unit 20 side of the gas / gas heater must be a two-series operation and the reheater 26 side must be a one-series operation. (1) Stop series reheater However, there is a problem that (2) the exhaust gas temperature after reheating on the operating side is low (the amount of heat exchange is about half). (B) Single-system operation of whole system Since the above-mentioned problem is present in the single-system operation of desulfurization, it may be possible to operate the whole system including denitration as a single-system operation, but in this case, there is the following problem. That is, although the amount of exhaust gas to be treated is the planned amount, the temperature is low because the load is low. This means that in denitration using a catalyst, the denitration performance deteriorates, and when planning such an operation from the beginning, it is necessary to increase the amount of catalyst in advance, resulting in an increase in cost.
【００１０】本発明は上記の諸点に鑑みなされたもの
で、本発明の目的は、上記の問題点をすべて解消し、か
つ経済的にも優れた排煙処理方法及び装置を提供するこ
とにある。また、本発明の他の目的は、排ガス中に含ま
れる水銀、ダイオキシンなどの有害物質を除塵と同時に
吸着・除去することができる排煙処理方法及び装置を提
供することにある。The present invention has been made in view of the above points, and an object of the present invention is to provide a method and apparatus for flue gas treatment which solves all of the above problems and is economically excellent. . Another object of the present invention is to provide a flue gas treatment method and apparatus capable of adsorbing and removing harmful substances such as mercury and dioxins contained in exhaust gas simultaneously with dust removal.
【００１１】[0011]
【課題を解決するための手段】上記の目的を達成するた
めに、本発明の排煙処理方法は、石炭燃焼排ガスを脱硝
処理した後、空気予熱器に導入して熱回収し、ついで、
冷却された排ガスを集じん機に導入して集塵した後、媒
体循環式のガス・ガスヒータの熱回収器に導入して冷却
し、ついで、冷却された排ガスを湿式石灰石膏法により
脱硫処理した後、前記媒体循環式のガス・ガスヒータの
再加熱器に導入し再加熱して煙突に導く排煙処理方法に
おいて、集じん機にはバグフィルターを、媒体循環式の
ガス・ガスヒータの熱回収器に耐熱・耐酸性合成樹脂製
チューブとしてテフロンチューブを用いるように構成し
たものである。In order to achieve the above object, the flue gas treatment method of the present invention is a method for denitrifying coal combustion exhaust gas, which is then introduced into an air preheater to recover heat.
After the cooled exhaust gas is introduced into the dust collector to collect dust, it is introduced into the heat recovery device of the medium circulation type gas / gas heater to cool it, and then the cooled exhaust gas is processed by the wet lime gypsum method. > After desulfurization treatment, the flue gas treatment method is introduced to the reheater of the medium circulation type gas / gas heater and reheated to lead to the chimney.
In addition, a bag filter on the dust collector
Made of heat-resistant and acid-resistant synthetic resin for heat recovery device of gas and gas heater
It is configured to use a Teflon tube as the tube .
【００１２】上記の方法において、バグフィルター導入
前の排ガスにプレコート剤を混入することが好ましい。
プレコート剤としては、粉末活性炭、粉末活性コーク
ス、粉末消石灰、粉末生石灰、粉末石灰石及びフライア
ッシュの群からなる物質より選ばれた少なくとも一種が
用いられる。プレコート剤の添加量は、濾布上に５〜４
０g／m2の積層を形成させるように決定する。プレコー
ト剤添加量が上記の範囲未満の場合は、プレコート剤の
積層が不均一となり、ショートパスによる性能低下及び
濾布の目詰まりによる圧力損失増加の原因となる。一
方、上記の範囲を超える場合は、プレコート剤添加用装
置が過大となり、かつ、ダスト払い落としの頻度が多く
なるため、逆洗用加圧空気の消費量が増加して経済的で
ない。また、耐熱・耐酸性合成樹脂製チューブを定期的
に水洗浄するように構成することが好ましい。In the above method, it is preferable to mix a precoating agent into the exhaust gas before introducing the bag filter.
As the precoat agent, at least one selected from the group consisting of powdered activated carbon, powdered activated coke, powdered slaked lime, powdered quick lime, powdered limestone and fly ash is used. The amount of precoat agent added is 5-4 on the filter cloth.
It is determined to form a stack of 0 g / m 2 . If the amount of the precoating agent added is less than the above range, the precoating agent will not be laminated uniformly, which will cause a decrease in performance due to a short pass and an increase in pressure loss due to clogging of the filter cloth. On the other hand, when the amount exceeds the above range, the precoating agent adding device becomes excessively large, and the dust is frequently wiped off, so that the consumption amount of the backwashing pressurized air increases, which is not economical. Further, it is preferably configured to periodically water wash resistance heat and oxidation resistant synthetic resin tube.
【００１３】本発明の排煙処理装置は、石炭燃焼排ガス
を脱硝処理する脱硝装置と、脱硝された排ガスと燃焼用
空気とを熱交換する空気予熱器と、この空気予熱器から
の排ガスを集塵処理する集じん機と、脱塵された排ガス
の熱を回収する媒体循環式のガス・ガスヒータの熱回収
器と、この熱回収器からの排ガスを湿式石灰石膏法によ
り脱硫処理する脱硫装置と、脱硫された排ガスを再加熱
する前記媒体循環式のガス・ガスヒータの再加熱器と、
再加熱された排ガスを大気に排出する煙突とからなる排
煙処理装置において、前記集じん機はバグフィルターで
あり、前記媒体循環式のガス・ガスヒータの熱回収器
は、耐熱・耐酸性合成樹脂製チューブであるテフロンチ
ューブを備えていることを特徴としている。The flue gas treatment apparatus of the present invention is a denitration apparatus for denitrifying coal combustion exhaust gas, an air preheater for exchanging heat between the denitrated exhaust gas and combustion air, and an exhaust gas from this air preheater. A dust collector for dust treatment, a heat recovery device for a medium circulation gas / gas heater that recovers the heat of the exhaust gas that has been dedusted, and the exhaust gas from this heat recovery device by the wet lime gypsum method.
A desulfurization apparatus for desulfurizing Ri, and reheater of the medium circulation type gas-gas heater for re-heating the desulfurized flue gas,
Ing reheated exhaust gases from the chimney to discharge into the atmosphere the exhaust
In the smoke treatment device, the dust collector is a bag filter.
There, the heat recovery unit of the gas-gas heater of the medium circulation type is a heat and oxidation resistant synthetic resin tube Tefuronchi
It is characterized by having a tube .
【００１４】上記の装置において、バグフィルターをガ
ス流れに対して並列に複数区画に分割し、各区画の出口
に煤塵濃度検出器を、各区画の入口及び出口の少なくと
も一方にガス遮断手段を設けることが好ましい。濾布の
破損が起こった場合、煤塵濃度の高いガスが洩れること
により、煤塵の排出規制値が守れなくなることを防止す
る必要がある。このため、複数区画に分割し、濾布の破
損部のみを遮断して、運転を継続することができ、遮断
した区画の濾布取替えを運転中に可能とする。さらに、
ガス・ガスヒータの熱回収器内をガス流れに対して並列
に複数区画に分割し、各区画に洗浄水供給管を接続する
ことが好ましい。熱回収器全体を一時に洗浄すると、ガ
スの冷却が起こり、排ガスの再加熱が不充分となる。し
たがって、複数区画に分割してサイクリックに洗浄する
ことにより、ガス冷却の効果を軽減する。この場合ガス
・ガスヒータの熱回収器の各区画と脱硫装置とを、使用
済洗浄水管を介して接続することが好ましい。[0014] In the above apparatus, the bugs filter is divided into a plurality sections in parallel with respect to the gas flow, the dust concentration detector at the outlet of each compartment, the gas blocking means on at least one of the inlet and outlet of each compartment It is preferable to provide. When the filter cloth is damaged, it is necessary to prevent the gas emission with a high dust concentration from leaking and failing to comply with the emission control value of the dust. Therefore, the operation can be continued by dividing the filter cloth into a plurality of sections and cutting off only the damaged portion of the filter cloth, and the filter cloth in the blocked section can be replaced during the operation. further,
It is preferable to divide the inside of the heat recovery unit of the gas / gas heater into a plurality of sections in parallel with the gas flow, and connect the cleaning water supply pipe to each section. If the entire heat recovery device is washed at one time, cooling of the gas occurs and reheating of the exhaust gas becomes insufficient. Therefore, the effect of gas cooling is reduced by dividing into a plurality of compartments and cyclically cleaning. In this case, it is preferable to connect each section of the heat recovery device of the gas / gas heater and the desulfurization device via a used washing water pipe.
【００１５】[0015]
【発明の実施の形態】図１は、本発明の排煙処理方法を
実施する装置の一実施例を示している。石炭焚燃焼装
置、例えば石炭焚ボイラ１０からの排ガスは、脱硝装置
１２に導入されて脱硝された後、空気予熱器１４に導入
して熱回収され、ついで熱回収後の冷却された排ガスは
バグフィルター１７に導入されて集塵された後、媒体、
例えば水を循環する媒体循環式のガス・ガスヒータ１８
ａの熱回収部２０ａに導入される。空気予熱器１４出口
とバグフィルター１７入口との間の排ガスにプレコート
剤が添加される。プレコート剤は粉末活性炭、粉末活性
コークス、粉末消石灰、粉末生石灰、粉末石灰石もしく
はフライアッシュ又はこれらの混合物である。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS FIG. 1 shows an embodiment of an apparatus for carrying out the flue gas treatment method of the present invention. Exhaust gas from a coal-fired combustion device, for example, a coal-fired boiler 10 is introduced into a denitration device 12 and denitrated, and then introduced into an air preheater 14 to recover heat, and then the cooled exhaust gas after the heat recovery is a bag. After being introduced into the filter 17 to collect dust, the medium,
For example, a medium circulation type gas / gas heater 18 for circulating water
a is introduced into the heat recovery section 20a. The precoat agent is added to the exhaust gas between the outlet of the air preheater 14 and the inlet of the bag filter 17. The precoat agent is powdered activated carbon, powdered activated coke, powdered slaked lime, powdered quicklime, powdered limestone or fly ash, or a mixture thereof.
【００１６】ガス・ガスヒータ１８ａの熱回収器２０ａ
は、耐熱・耐酸性合成樹脂製チューブとしてテフロンチ
ューブから構成されており、熱回収器２０ａで冷却され
た排ガスは湿式石灰石膏法脱硫装置２４に導入されて脱
硫された後、媒体循環式のガス・ガスヒータの再加熱器
２６に導入され再加熱されて煙突２８から排出される。
なお、ガス・ガスヒータ１８ａは、熱回収器２０ａ及び
再加熱器２６から構成される。Heat recovery unit 20a of gas / gas heater 18a
Is composed of a Teflon tube as a heat-resistant and acid-resistant synthetic resin tube , and the exhaust gas cooled by the heat recovery device 20a is introduced into the wet lime gypsum method desulfurization device 24 to be desulfurized, and then a medium circulation type gas. -Introduced into the reheater 26 of the gas heater, reheated and discharged from the chimney 28.
The gas / gas heater 18a includes a heat recovery unit 20a and a reheating unit 26.
【００１７】バグフィルター１７は、図２〜図４に示す
ように、ガス流れに対して並列に区画隔壁４６により複
数の区画４８に分割され、各区画４８の出口に煤塵濃度
検出器５０が設けられ、各区画４８の入口及び出口にバ
ルブ、スライドダンパー等のガス遮断手段５２が設けら
れている。図２及び図３では、区画４８の入口及び出口
の両方にガス遮断手段５２を設ける場合を示している
が、いずれか一方のみにガス遮断手段を設けてもよい。
５４はバグフィルター本体、５６は濾布エレメント、５
８はガス入口、６０はガス出口、６２は逆洗用空気ノズ
ルである。As shown in FIGS. 2 to 4, the bag filter 17 is divided into a plurality of compartments 48 in parallel with a gas flow by a compartment partition wall 46, and a dust concentration detector 50 is provided at the outlet of each compartment 48. A gas shutoff means 52 such as a valve and a slide damper is provided at the entrance and the exit of each section 48. Although FIGS. 2 and 3 show the case where the gas blocking means 52 is provided at both the inlet and the outlet of the compartment 48, the gas blocking means may be provided at only one of them.
54 is a bag filter main body, 56 is a filter cloth element, 5
8 is a gas inlet, 60 is a gas outlet, and 62 is a backwashing air nozzle.
【００１８】ガス・ガスヒータの熱回収器２０ａは、図
５及び図６に示すように、ガス流れに対してバルブ、ス
ライドダンパー等のガス遮断手段３６、仕切部材３８に
より複数の区画４０に分割され、各区画４０に洗浄水供
給管４２が接続され、各区画４０と湿式石灰石膏法脱硫
装置２４とが使用済洗浄水管４３を介して接続されてい
る。４４は洗浄水ノズル、４５はチューブである。チュ
ーブ４５は、各区画４０毎に定期的に水洗浄される。As shown in FIGS. 5 and 6, the heat recovery unit 20a of the gas / gas heater is divided into a plurality of compartments 40 by a gas shutoff means 36 such as a valve and a slide damper, and a partition member 38 for the gas flow. A washing water supply pipe 42 is connected to each section 40, and each section 40 and the wet lime gypsum method desulfurization device 24 are connected via a used washing water tube 43. 44 is a washing water nozzle, and 45 is a tube. The tube 45 is regularly washed with water for each section 40.
【００１９】図７は、図１に示す装置を２系列接続し
て、片系列運転又は２系列運転を行なうことができるよ
うに構成した例を示している。なお、誘引ファン及びブ
ースタファンの図示を省略している。図８は従来方法に
おける電気集塵機のフライアッシュ電気抵抗値と集塵効
率との関係を示している。図８から、フライアッシュ電
気抵抗値が大きくなるにつれて、集塵効率が大きく低下
することがわかるが、バグフィルターを用いる場合は、
このような現象は生じない。FIG. 7 shows an example in which the apparatus shown in FIG. 1 is connected in two lines so that one-side operation or two-line operation can be performed. The attraction fan and booster fan are not shown. FIG. 8 shows the relationship between the fly ash electric resistance value and the dust collection efficiency of the electric dust collector in the conventional method. It can be seen from FIG. 8 that the dust collection efficiency is significantly reduced as the fly ash electric resistance value is increased.
Such a phenomenon does not occur.
【００２０】上記のように構成された排煙処理装置にお
いて、石炭焚ボイラ１０からの排ガスを脱硝装置１２に
導入して排ガス中のＮＯｘを除去した後、空気予熱器１
４に導入して燃焼用空気を予熱し、ついで、熱回収後の
冷却された排ガスにプレコート剤を添加してバグフィル
ターに導入して集塵する。図９及び図１０に示すような
従来方式では、ガス・ガスヒータ入口のダスト（煤塵）
濃度が高いため、ガス・ガスヒータで冷却されて生成す
るＳＯ3 、硫安又は酸性硫安の大部分がダスト表面に付
着し、除塵塔（脱塵塔）や脱硫装置でかなりの部分が捕
集されるのに対し、バグフィルターで高性能除塵を行わ
せることにより、これらの生成物がヒューム状又は浮遊
ダストになり、脱硫装置で捕集されず煙突から排出され
ることが懸念される。これらの問題は、バグフィルター
１７の前の排ガスに粉末活性炭、粉末活性コークス、粉
末消石灰、粉末生石灰、粉末石灰石もしくはフライアッ
シュ又はこれらの混合物からなるプレコート剤を混入さ
せることにより解決できる。すなわち、プレコート剤に
よりガス中のＳＯ3 が物理的又は化学的に吸着・除去さ
れる。また、粉末活性炭又は粉末活性コークスを使用す
る場合には、蒸気で存在する水銀、ダイオキシンなどの
有害物質も同時に吸着・除去される。なお、粉末消石
灰、粉末生石灰又は粉末石灰石を使用する場合でも、凝
縮している水銀等の有害物質は除去される。また、プレ
コート剤の使用により、濾布の目詰まりを防止し、圧力
損失の増加を防ぐことができる。In the flue gas treatment apparatus constructed as described above, after the exhaust gas from the coal-fired boiler 10 is introduced into the denitration device 12 to remove NOx in the exhaust gas, the air preheater 1
4, the combustion air is preheated, and then the pre-coating agent is added to the cooled exhaust gas after heat recovery and introduced into a bag filter to collect dust. In the conventional method as shown in FIGS. 9 and 10, dust at the gas / gas heater inlet (soot dust)
Since the concentration is high, most of the SO 3 , ammonium sulfate or ammonium sulfate that is generated by cooling with the gas / gas heater adheres to the dust surface, and a considerable portion is collected by the dust removal tower (dedusting tower) or desulfurization equipment. On the other hand, by performing high-performance dust removal with a bag filter, it is feared that these products become fume-like or floating dust and are not collected by the desulfurization device and discharged from the stack. These problems can be solved by mixing a pre-coating agent made of powdered activated carbon, powdered activated coke, powdered lime, powdered lime, powdered limestone or fly ash, or a mixture thereof into the exhaust gas in front of the bag filter 17. That is, SO 3 in the gas is physically or chemically adsorbed / removed by the precoating agent. When powdered activated carbon or powdered activated coke is used, harmful substances such as mercury and dioxins existing in vapor are also adsorbed and removed at the same time. Even when powdered slaked lime, powdered quick lime, or powdered limestone is used, condensed harmful substances such as mercury are removed. In addition, the use of the precoat agent can prevent clogging of the filter cloth and increase in pressure loss.
【００２１】バグフィルター１７で除塵された排ガス
は、媒体循環式のガス・ガスヒータの熱回収器２０ａに
導入されて冷却され、ついで、冷却された排ガスは脱硫
装置２４に導入されて排ガス中のＳＯｘが除去された
後、媒体循環式のガス・ガスヒータの再加熱器２６に導
入されて再加熱され煙突２８へ導かれる。ガス・ガスヒ
ータの熱回収器２０ａは、耐熱・耐酸性合成樹脂製チュ
ーブであるテフロンチューブで構成されているので、腐
食の心配はなく、バグフィルター１７出口の煤塵濃度を
低くすることができる。The exhaust gas dedusted by the bag filter 17 is introduced into the heat recovery unit 20a of the medium circulation type gas / gas heater to be cooled, and then the cooled exhaust gas is introduced into the desulfurization unit 24 and SOx in the exhaust gas. After being removed, the gas is introduced into the reheater 26 of the medium circulation type gas / gas heater, reheated and guided to the chimney 28. Heat recovery unit 20a of the gas-gas heater, which is configured in a Teflon tube which is resistant to heat and oxidation resistant synthetic resin tube, no fear of corrosion, it is possible to lower the dust concentration of the bag filter 17 outlet.
【００２２】[0022]
【発明の効果】本発明は上記のように構成されているの
で、つぎのような効果を奏する。
（１） バグフィルターは電気集塵機と比較して除塵性
能がきわめて高く（石炭の品質に左右されない）、厳し
い煤塵排出規制を満足することができる。その反面、ガ
ス・ガスヒータの熱回収部で凝縮するＳＯ3 がアルカリ
性のダストで中和されないため腐食の問題が発生する。
また、脱硝部で未反応のアンモニアと反応して生成する
硫安又は酸性硫安がチューブに付着するため、伝熱抵抗
となり性能低下につながる問題がある。なお、従来の剛
球（鋼球）散布方式では、これら付着物質の除去は困難
である。水洗浄を併用することは可能であるが、厳しい
腐食問題が生じる。本発明では、バグフィルターを用
い、かつ、ガス・ガスヒータの熱回収部は、耐食性に優
れたテフロンからなる耐熱・耐酸性合成樹脂製チューブ
で構成されているので、腐食のおそれはなく、バグフィ
ルター出口の煤塵濃度を低くすることができる。
（２） ガス・ガスヒータの熱回収部のチューブを各区
画毎に定期的に水洗浄することができるように構成する
場合は、（１）の効果をさらに発揮させることができ
る。
（３） バグフィルター前の排ガスにプレコート剤を添
加することにより、ガス中のＳＯ3 が物理的又は化学的
に吸着・除去されるとともに、ガス中の水銀、ダイオキ
シンなどの有害物質を吸着・除去することができる。と
くに、プレコート剤として粉末活性炭又は粉末活性コー
クスを使用する場合は、蒸気で存在する水銀、ダイオキ
シンを効率よく吸着・除去することができる。また、プ
レコート剤の使用により、濾布の目詰まりを防止し、圧
力損失の増加を防ぐことができる。
（４） バグフィルターの濾布が破損した場合に、排ガ
ス中の煤塵濃度が増加することが懸念されるが、バグフ
ィルターを複数の区画に分割し、各区画の出口に煤塵濃
度検出器を設ける場合は、煤塵濃度を検出して濾布破損
時に、その区画を遮断することにより、上記問題を解決
することができる。
（５） 脱硫装置入口での煤塵濃度が低く、さらに脱硫
装置でも集塵できるので、従来方式のように湿式電気集
塵機を設置しなくても煙突出口の煤塵濃度を低くするこ
とができる。
（６） 脱硫装置入口の煤塵濃度が低いため、従来方式
のように除塵塔を設置しなくても高品質の石膏が副生す
るので、設備が簡略化される。
（７） ガス・ガスヒータの熱回収器での煤塵濃度が低
く、かつ、熱交換チューブとしてテフロンを用いること
により、鋼管に比べ表面が滑らかであり、煤塵が付着し
にくいので、水洗装置などの簡単な除去装置により閉
塞、圧力損失の増加又は伝熱性能の低下を防止すること
ができる。
（８） ボイラ誘引ファンを設置するバグフィルター出
口はガス温度が高く、酸露点温度以上であるため腐食の
心配が無く、誘引ファンに耐食材料を使用する必要がな
い。
（９） ２系列時の運用についても、最も片系列運転の
頻度が高いと予想される脱硫装置は、ガス・ガスヒータ
を含め最下流に位置しており、片系列運用が容易に行え
る。Since the present invention is configured as described above, it has the following effects. (1) The bag filter has extremely high dust removal performance (not affected by coal quality) as compared with an electric dust collector, and can satisfy strict dust emission regulations. On the other hand, SO 3 condensed in the heat recovery section of the gas / gas heater is not neutralized by the alkaline dust, which causes a problem of corrosion.
Further, since ammonium sulfate or acidic ammonium sulfate generated by reacting with unreacted ammonia in the denitration part adheres to the tube, there is a problem that it becomes a heat transfer resistance and leads to performance deterioration. Note that it is difficult to remove these adhered substances by the conventional hard ball (steel ball) spraying method. It is possible to use water washing together, but severe corrosion problems occur. In the present invention, since the bag filter is used, and the heat recovery part of the gas / gas heater is composed of a heat-resistant and acid-resistant synthetic resin tube made of Teflon having excellent corrosion resistance, there is no risk of corrosion, and the bag filter The dust concentration at the outlet can be reduced. (2) When the tube of the heat recovery part of the gas / gas heater is configured so that it can be regularly washed with water for each section, the effect of (1) can be further exerted. (3) By adding a pre-coating agent to the exhaust gas before the bag filter, SO 3 in the gas is physically or chemically adsorbed and removed, and harmful substances such as mercury and dioxin in the gas are also adsorbed and removed. can do. In particular, when powdered activated carbon or powdered activated coke is used as the precoating agent, mercury and dioxins existing in vapor can be efficiently adsorbed and removed. In addition, the use of the precoat agent can prevent clogging of the filter cloth and increase in pressure loss. (4) If the filter cloth of the bag filter is damaged, the dust concentration in the exhaust gas may increase, but the bag filter is divided into multiple sections, and a dust concentration detector is installed at the outlet of each section. In this case, the above problem can be solved by detecting the dust concentration and blocking the section when the filter cloth is damaged. (5) The soot concentration at the inlet of the desulfurization device is low, and since the dust can be collected by the desulfurization device, it is possible to reduce the soot concentration at the smoke outlet without installing a wet electrostatic precipitator as in the conventional method. (6) Since the dust concentration at the inlet of the desulfurizer is low, high-quality gypsum is by-produced without installing a dust removal tower as in the conventional method, so that the facility is simplified. (7) low dust concentration in the heat recovery unit of the gas-gas heater, and the use of Teflon as a heat exchange tubes
As a result , the surface is smoother than that of a steel pipe, and soot and dust are less likely to adhere to it. Therefore, a simple removing device such as a water washing device can prevent clogging, increase in pressure loss, or decrease in heat transfer performance. (8) Since the gas temperature at the bag filter outlet where the boiler induction fan is installed is high and is higher than the acid dew point temperature, there is no fear of corrosion and it is not necessary to use a corrosion resistant material for the induction fan. (9) As for the operation of two series, the desulfurization equipment, which is expected to have the highest frequency of single series operation, is located at the most downstream side including the gas and gas heaters, and the single series operation can be easily performed.
【図１】本発明の排煙処理装置の一実施例を示す系統図
である。FIG. 1 is a system diagram showing an embodiment of a smoke treatment apparatus of the present invention.
【図２】図１におけるバグフィルターの一例を示す平面
図である。FIG. 2 is a plan view showing an example of a bag filter in FIG.
【図３】図２におけるＡ−Ａ線断面図である。3 is a cross-sectional view taken along the line AA in FIG.
【図４】図２におけるＢ−Ｂ線断面図である。FIG. 4 is a sectional view taken along line BB in FIG.
【図５】図１におけるガス・ガスヒータの熱回収器の一
例を示す立面断面図である。5 is an elevational sectional view showing an example of a heat recovery unit of the gas / gas heater in FIG.
【図６】同平面断面図である。FIG. 6 is a cross-sectional view of the same plane.
【図７】図１に示す装置を２系列接続した装置の一例を
示す系統図である。FIG. 7 is a system diagram showing an example of a device in which two devices shown in FIG. 1 are connected in series.
【図８】従来方式における電気集塵機のフライアッシュ
電気抵抗値と集塵効率との関係を示すグラフである。FIG. 8 is a graph showing a relationship between fly ash electric resistance value and dust collection efficiency of a conventional electrostatic precipitator.
【図９】従来の排煙処理装置の一例を示す系統図であ
る。FIG. 9 is a system diagram showing an example of a conventional flue gas treatment device.
【図１０】従来の排煙処理装置の他の例を示す系統図で
ある。FIG. 10 is a system diagram showing another example of a conventional flue gas treatment device.
【図１１】従来の排煙処理装置のさらに他の例を示す系
統図である。FIG. 11 is a system diagram showing still another example of a conventional flue gas treatment device.
【図１２】図１１に示す装置を２系列接続した装置の系
統図である。FIG. 12 is a system diagram of a device in which two devices shown in FIG. 11 are connected in series.
１０ 石炭焚ボイラ １２ 脱硝装置 １４ 空気予熱器 １７ バグフィルター １８ａ ガス・ガスヒータ ２０ａ 熱回収器 ２２ 脱塵塔 ２４ 脱硫装置 ２６ 再加熱器 ２８ 煙突 ３０ 湿式電気集じん機 ３２ 誘引ファン ３４ ブースタファン ３６ ガス遮断手段 ３８ 仕切部材 ４０ 区画 ４２ 洗浄水供給管 ４３ 使用済洗浄水管 ４４ 洗浄水ノズル ４５ チューブ ４６ 区画隔壁 ４８ 区画 ５０ 煤塵濃度検出器 ５２ ガス遮断手段 ５４ バグフィルター本体 ５６ 濾布エレメント ５８ ガス入口 ６０ ガス出口 ６２ 逆洗用空気ノズル 10 coal-fired boiler 12 Denitration equipment 14 Air preheater 17 Bug Filter 18a gas / gas heater 20a heat recovery device 22 Dedusting tower 24 Desulfurization equipment 26 Reheater 28 chimney 30 Wet electric dust collector 32 Attraction Fan 34 booster fans 36 Gas shutoff means 38 Partition member 40 divisions 42 Wash water supply pipe 43 Used cleaning water pipe 44 Wash water nozzle 45 tubes 46 partition walls 48 divisions 50 Dust concentration detector 52 Gas shutoff means 54 Bag filter body 56 Filter element 58 gas inlet 60 gas outlet 62 Air nozzle for backwash
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ Ｂ０１Ｄ 53/77 Ｆ２３Ｊ 15/00 Ｂ Ｆ２３Ｊ 15/00 Ｚ (72)発明者 亀田 孝志 神戸市中央区東川崎町３丁目１番１号 川崎重工業株式会社 神戸工場内 (72)発明者 片岡 重則 神戸市中央区東川崎町３丁目１番１号 川崎重工業株式会社 神戸工場内 (56)参考文献 特開 昭59−90618（ＪＰ，Ａ) 特開 平４−341320（ＪＰ，Ａ) 特開 平７−308540（ＪＰ，Ａ) 特開 平８−152127（ＪＰ，Ａ) 実開 昭58−93641（ＪＰ，Ｕ) (58)調査した分野(Int.Cl.7，ＤＢ名) B01D 53/34 ─────────────────────────────────────────────────── ─── Continuation of front page (51) Int.Cl. 7 Identification code FI B01D 53/77 F23J 15/00 B F23J 15/00 Z (72) Inventor Takashi Kameda 3-1-1 Higashikawasaki-cho, Chuo-ku, Kobe No. Kawasaki Heavy Industries, Ltd. Kobe factory (72) Inventor Shigenori Kataoka 3-1-1 Higashikawasaki-cho, Chuo-ku, Kobe Kawasaki Heavy Industries Ltd., Kobe factory (56) Reference JP-A-59-90618 (JP, A) JP-A-4-341320 (JP, A) JP-A-7-308540 (JP, A) JP-A-8-152127 (JP, A) Actual development Sho-58-93641 (JP, U) (58) Fields investigated (Int.Cl. 7 , DB name) B01D 53/34
Claims (7)
予熱器に導入して熱回収し、ついで、冷却された排ガス
を集じん機に導入して集塵した後、媒体循環式のガス・
ガスヒータの熱回収器に導入して冷却し、ついで、冷却
された排ガスを湿式石灰石膏法により脱硫処理した後、
前記媒体循環式のガス・ガスヒータの再加熱器に導入し
再加熱して煙突に導く排煙処理方法において、 集じん機にはバグフィルターを、媒体循環式のガス・ガ
スヒータの熱回収器に耐熱・耐酸性合成樹脂製チューブ
としてテフロンチューブを用いる ことを特徴とする排煙
処理方法。1. After denitrifying the coal combustion exhaust gas, it is introduced into an air preheater to recover heat, and then the cooled exhaust gas is introduced into a dust collector to collect dust , followed by a medium circulation type gas.
After being introduced into the heat recovery device of the gas heater and cooled, and then the cooled exhaust gas is desulfurized by the wet lime gypsum method ,
In the flue gas treatment method of introducing into the reheater of the medium circulation type gas / gas heater and reheating to lead to the chimney, a bag filter is provided in the dust collector and a medium circulation type gas / gas
Heat-resistant and acid-resistant synthetic resin tube for the heat recovery device of the heater
A flue gas treatment method that uses a Teflon tube as the .
ート剤を混入する請求項１記載の排煙処理方法。2. The flue gas treatment method according to claim 1, wherein a precoating agent is mixed into the exhaust gas before introduction of the bag filter.
ークス、粉末消石灰、粉末生石灰、粉末石灰石及びフラ
イアッシュの群からなる物質より選ばれた少なくとも一
種である請求項２記載の排煙処理方法。 3. The flue gas treatment method according to claim 2, wherein the precoating agent is at least one selected from the group consisting of powdered activated carbon, powdered activated coke, powdered slaked lime, powdered quick lime, powdered limestone and fly ash .
的に水洗浄する請求項１、２又は３記載の排煙処理方
法。4. The flue gas treatment method according to claim 1 , 2 or 3, wherein the heat-resistant and acid-resistant synthetic resin tube is periodically washed with water.
と、 脱硝された排ガスと燃焼用空気とを熱交換する空気予熱
器と、 この空気予熱器からの排ガスを集塵処理する集じん機
と、 脱塵された排ガスの熱を回収する媒体循環式のガス・ガ
スヒータの熱回収器と、 この熱回収器からの排ガスを湿式石灰石膏法により脱硫
処理する脱硫装置と、 脱硫された排ガスを再加熱する前記媒体循環式のガス・
ガスヒータの再加熱器と、 再加熱された排ガスを大気に排出する煙突とからなる排
煙処理装置において、前記集じん機はバグフィルターであり、 前記媒体循環式
のガス・ガスヒータの熱回収器は、耐熱・耐酸性合成樹
脂製チューブであるテフロンチューブを備えていること
を特徴とする排煙処理装置。5. A denitration device for denitrifying coal combustion exhaust gas.
When, Air preheating for heat exchange between denitration exhaust gas and combustion air
A vessel, Exhaust gas from this air preheater is treated to collect dustDust collector
When, A medium-circulation type gas / gas that recovers the heat of exhaust gas that has been dedusted
A heat recovery device for the heater The exhaust gas from this heat recovery unitBy wet lime gypsum methodDesulfurization
A desulfurization device for processing, The medium circulation type gas for reheating desulfurized exhaust gas
Gas heater reheater, It consists of a chimney that discharges the reheated exhaust gas to the atmosphere.Excretion
In smoke treatment equipment,The dust collector is a bag filter, The medium circulation type
The heat recovery unit of the gas and gas heater of
Fat tubeIs a Teflon tubeBe equipped with
A flue gas treatment device characterized by.
に複数区画に分割し、各区画の出口に煤塵濃度検出器
を、各区画の入口及び出口の少なくとも一方にガス遮断
手段を設けた請求項５記載の排煙処理装置。6. The bag filter is divided into a plurality of compartments in parallel to the gas flow, a soot concentration detector is provided at the outlet of each compartment, and a gas blocking means is provided at at least one of the inlet and the outlet of each compartment. The flue gas treatment device according to 5 .
れに対して並列に複数区画に分割し、各区画に洗浄水供
給管を接続した請求項５又は６記載の排煙処理装置。 7. A in the heat recovery unit of the gas-gas heater is divided into a plurality sections in parallel with respect to the gas flow, flue gas treatment apparatus according to claim 5 or 6, wherein connecting the cleaning water supply pipe in each compartment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP35321495A JP3423517B2 (en) | 1995-12-27 | 1995-12-27 | Exhaust gas treatment method and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP35321495A JP3423517B2 (en) | 1995-12-27 | 1995-12-27 | Exhaust gas treatment method and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH09173768A JPH09173768A (en) | 1997-07-08 |
| JP3423517B2 true JP3423517B2 (en) | 2003-07-07 |
Family
ID=18429335
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP35321495A Expired - Lifetime JP3423517B2 (en) | 1995-12-27 | 1995-12-27 | Exhaust gas treatment method and device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3423517B2 (en) |
Cited By (1)
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|---|---|---|---|---|
| CN102188863A (en) * | 2010-03-04 | 2011-09-21 | 天华化工机械及自动化研究设计院 | Process for preventing fogging and explosion of coal dried tail gas in dry bag-type dust removal process |
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1995
- 1995-12-27 JP JP35321495A patent/JP3423517B2/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102188863A (en) * | 2010-03-04 | 2011-09-21 | 天华化工机械及自动化研究设计院 | Process for preventing fogging and explosion of coal dried tail gas in dry bag-type dust removal process |
| CN102188863B (en) * | 2010-03-04 | 2013-05-15 | 天华化工机械及自动化研究设计院有限公司 | Process for preventing fogging and explosion of coal dried tail gas in dry bag-type dust removal process |
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| Publication number | Publication date |
|---|---|
| JPH09173768A (en) | 1997-07-08 |
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