JPH0635888B2 - Garbage incineration plant - Google Patents
Garbage incineration plantInfo
- Publication number
- JPH0635888B2 JPH0635888B2 JP2000990A JP99090A JPH0635888B2 JP H0635888 B2 JPH0635888 B2 JP H0635888B2 JP 2000990 A JP2000990 A JP 2000990A JP 99090 A JP99090 A JP 99090A JP H0635888 B2 JPH0635888 B2 JP H0635888B2
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- temperature
- heat exchanger
- white smoke
- bag filter
- 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
- 239000010813 municipal solid waste Substances 0.000 title description 2
- 238000001816 cooling Methods 0.000 claims description 20
- 238000006243 chemical reaction Methods 0.000 claims description 17
- 230000002378 acidificating effect Effects 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 230000003472 neutralizing effect Effects 0.000 claims description 3
- 238000004056 waste incineration Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 115
- 239000000779 smoke Substances 0.000 description 38
- 230000002265 prevention Effects 0.000 description 21
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 18
- 238000002485 combustion reaction Methods 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 11
- 229910052753 mercury Inorganic materials 0.000 description 11
- 239000000428 dust Substances 0.000 description 9
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 8
- 239000004744 fabric Substances 0.000 description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 5
- 230000007423 decrease Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 4
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 4
- 230000006698 induction Effects 0.000 description 4
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- 239000004071 soot Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 4
- 239000003513 alkali Substances 0.000 description 3
- 239000012717 electrostatic precipitator Substances 0.000 description 3
- 229910052815 sulfur oxide Inorganic materials 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 235000011116 calcium hydroxide Nutrition 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 150000002013 dioxins Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000003365 glass fiber Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000009270 solid waste treatment Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000013076 target substance Substances 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Chimneys And Flues (AREA)
- Treating Waste Gases (AREA)
Description
【発明の詳細な説明】 〔産業上の利用分野〕 この発明は、都市ごみ焼却炉等の焼却炉から排出された
排ガスを処理する排ガス処理装置を備えたごみ焼却プラ
ントに関する。Description: TECHNICAL FIELD The present invention relates to a refuse incineration plant provided with an exhaust gas treatment device for treating exhaust gas discharged from an incinerator such as an municipal incinerator.
近年、都市ごみ処理は焼却処理が主流となっている。焼
却によって排出される排ガスの中には、煤塵を始め、塩
化水素（ＨＣｌ）、硫黄酸化物（ＳＯＸ）、窒素酸化物
（ＮＯＸ）などの有害物質が多量に含まれており、ごみ
焼却に伴う二次公害の発生を防止するために、これらの
物質を効率的且つ効果的に除去することのできる排ガス
処理装置の開発が求められる一方で、大気汚染防止対策
としてこれらの物質の排出濃度が厳しく規制されてい
る。In recent years, incineration has become the mainstream for municipal solid waste treatment. Exhaust gas discharged by incineration contains a large amount of harmful substances such as soot dust, hydrogen chloride (HCl), sulfur oxides (SO x ), nitrogen oxides (NO x ), etc. In order to prevent the occurrence of secondary pollution due to the pollution, it is required to develop an exhaust gas treatment device that can remove these substances efficiently and effectively. Is strictly regulated.
従来、都市ごみ焼却炉から排出された排ガスを処理する
排ガス処理装置を備えたごみ焼却プラントとしては、例
えば、第３図に示すようなものが知られている。BACKGROUND ART Conventionally, as a refuse incineration plant equipped with an exhaust gas treating apparatus for treating exhaust gas discharged from an incinerator for municipal waste, for example, one shown in FIG. 3 is known.
このごみ焼却プラントは、焼却炉１、該焼却炉１から排
出された高温の排ガスを冷却する冷却装置２、該冷却装
置２から導入された排ガスで熱交換して白煙防止用加熱
空気を排出する白煙防止用熱交換器３、熱交換された排
ガス中の酸性成分を中和反応させる反応塔５、該反応塔
５の下流側に設けられた集塵器３０、該集塵器３０から
の排ガスを還元脱硝する脱硝装置８、該脱硝装置８から
導入された排ガスと上記白煙防止用加熱空気とを混合す
る混合器１０から構成されている。This refuse incineration plant discharges white smoke prevention heated air by exchanging heat with an incinerator 1, a cooling device 2 for cooling high-temperature exhaust gas discharged from the incinerator 1, and an exhaust gas introduced from the cooling device 2. From the white smoke prevention heat exchanger 3, the reaction tower 5 for neutralizing the acid components in the heat-exchanged exhaust gas, the dust collector 30 provided on the downstream side of the reaction tower 5, and the dust collector 30 A denitration device 8 for reducing and denitrifying the exhaust gas, and a mixer 10 for mixing the exhaust gas introduced from the denitration device 8 and the heated air for preventing white smoke.
また、白煙防止用熱交換器３と集塵器３０との間には燃
焼空気用熱交換４が設けられている。更に、脱硝装置８
からの排ガスを吸引して混合器１０へ送る誘引送風機
９、混合器１０へ導入された排ガスを大気中へ放出する
煙突１１なども有する。Further, a heat exchange 4 for combustion air is provided between the white smoke prevention heat exchanger 3 and the dust collector 30. Furthermore, denitration device 8
It also has an induction blower 9 that sucks the exhaust gas from the mixer and sends it to the mixer 10, and a chimney 11 that discharges the exhaust gas introduced into the mixer 10 into the atmosphere.
このごみ焼却プラントの処理フローは以下のようになっ
ている。The processing flow of this refuse incineration plant is as follows.
焼却炉１から排出された高温の排ガスは、冷却装置２で
冷却され、更に、白煙防止用熱交換器３及び燃焼空気用
熱交換器４で熱交換される。次に、反応塔５内で消石灰
などのアルカリ剤が噴霧され、排ガス中に含まれている
塩化水素などの酸性成分の有害物質は中和反応を起こ
し、その反応生成物は電気集塵器などの集塵器３０を通
過する際に煤塵と共に除去される。その後、煙道中にＮ
Ｈ３ガスを噴霧し、その下流側に設けた脱硝装置８で還
元脱硝を行う。これにより、排ガスから窒素酸化物が除
去されて、清浄化された排ガスが、誘引送風機９で吸引
されて混合器１０へと送られる。混合器１０では、白煙
防止用熱交換器３で得た白煙防止用の加熱空気を清浄化
された排ガスと混合して、排ガスの温度を上昇させる。
このように、清浄化された排ガスを、一旦加熱した上で
煙突１１より大気に放出するようにして、白煙の発生防
止が図られている。The high-temperature exhaust gas discharged from the incinerator 1 is cooled by the cooling device 2, and is further heat-exchanged by the white smoke prevention heat exchanger 3 and the combustion air heat exchanger 4. Next, an alkaline agent such as slaked lime is sprayed in the reaction tower 5, harmful substances of acidic components such as hydrogen chloride contained in the exhaust gas cause a neutralization reaction, and the reaction product is an electrostatic precipitator or the like. The dust is removed together with the soot when passing through the dust collector 30. After that, N in the flue
H 3 gas is sprayed, and reduction denitration is performed by the denitration device 8 provided on the downstream side. Thereby, nitrogen oxides are removed from the exhaust gas, and the cleaned exhaust gas is sucked by the induction blower 9 and sent to the mixer 10. In the mixer 10, the white smoke prevention heated air obtained in the white smoke prevention heat exchanger 3 is mixed with the purified exhaust gas to raise the temperature of the exhaust gas.
In this way, the purified exhaust gas is once heated and then released from the chimney 11 to the atmosphere, thereby preventing the generation of white smoke.
ところで、有害物質の規制は近年ますます強化される傾
向にあり、ダイオキシンや水銀などもその対象物質とな
ることが予想される。ダイオキシンの生成過程は明確に
は解明されていないが、３００℃前後の温度で電気集塵
器３０内で増成されることが確認されている。また、水
銀は３００℃の温度では気化状態にあるため電気集塵器
３０で捕捉することができないのが現状である。By the way, regulations on toxic substances have tended to be tightened in recent years, and it is expected that dioxin and mercury will also be the target substances. Although the production process of dioxin has not been clarified, it has been confirmed that dioxin is formed in the electrostatic precipitator 30 at a temperature of about 300 ° C. In addition, since mercury is in a vaporized state at a temperature of 300 ° C., it cannot be captured by the electrostatic precipitator 30 at present.
そこで、ダイオキシンの生成を抑制し、且つ凝縮するた
め、及び水銀の気化を避けるために排ガスの温度を下げ
る（１８０℃）と共に、水銀を除去するために微粒子に
付着した水銀粒子を捕捉することのできるバグフィルタ
を集塵器として採用することが考えられる。Therefore, the temperature of the exhaust gas is lowered (180 ° C.) in order to suppress and condense the production of dioxin and to avoid the vaporization of mercury, and at the same time, the mercury particles attached to the fine particles are trapped in order to remove the mercury. It is possible to adopt a bag filter that can be used as a dust collector.
しかしながら、排ガスの温度が低下すると、脱走装置８
の脱硝触媒の活性が低下するため、脱硝効率が大きく低
下してしまうという問題がある。例えば、排ガスの温度
が２１０℃〜２２０℃における脱硝率は約８０％である
のに対して、排ガスの温度が約１８５℃における脱硝率
は約６５％に低下してしまうのである。一方、脱硝装置
８を通過する排ガスの温度が低下すると、下流側の混合
器１０において、白煙防止用熱交換器３で得た高温の加
熱空気で排ガスの温度上昇を図っても、排ガス中の水分
率を低く抑えることができない。このため、排ガスが大
気へ放出される際に、飽和水蒸気に達して多量の水蒸
気、即ち、白煙が発生してしまうという問題点がでてく
る。However, when the temperature of the exhaust gas decreases, the escape device 8
Since the activity of the denitration catalyst of No. 1 is reduced, there is a problem that the denitration efficiency is greatly reduced. For example, the denitrification rate at an exhaust gas temperature of 210 ° C to 220 ° C is about 80%, whereas the denitrification rate at an exhaust gas temperature of about 185 ° C decreases to about 65%. On the other hand, when the temperature of the exhaust gas passing through the denitration device 8 decreases, even if the temperature of the exhaust gas is increased in the downstream mixer 10 by the high temperature heated air obtained by the white smoke prevention heat exchanger 3, It is not possible to keep the moisture content of the product low. Therefore, when the exhaust gas is discharged to the atmosphere, it reaches saturated steam and a large amount of steam, that is, white smoke is generated.
そこで、ダイオキシン及び水銀を除去し、脱硝効率の低
下及び白煙の発生を防止するためには、排ガスの温度
を、バグフィルタ通過時には低く、脱硝装置への導入時
には高くするという課題を解決することにより、脱硝効
率の向上及び白煙発生防止を図ると共に、ダイオキシン
及び水銀を除去することのできるごみ焼却プラントを提
供することである。Therefore, in order to remove dioxin and mercury, and to prevent the decrease of the denitration efficiency and the generation of white smoke, the problem that the temperature of the exhaust gas is low when passing through the bag filter and high when being introduced into the denitration device is solved. Accordingly, it is to provide a refuse incineration plant capable of removing dioxin and mercury while improving the denitration efficiency and preventing the generation of white smoke.
この発明は、上記目的を達成するため、次のように構成
されている。The present invention is configured as follows to achieve the above object.
即ち、この発明は、焼却炉から排出された高温の排ガス
を冷却する冷却装置、該冷却装置からの排ガスで加熱空
気を発生させる熱交換器、排ガス中の酸性成分を中和反
応させる反応塔、該反応塔の下流側に設けたバグフィル
タ、該バグフィルタからの排ガスを還元脱硝する脱硝装
置、前記バグフィルタと前記脱硝装置との間に配置した
前記加熱空気で前記排ガスを昇温する熱交換器、及び前
記脱硝装置からの排ガスと前記加熱空気とを混合する混
合器、を有するごみ焼却プラントに関する。That is, the present invention is a cooling device for cooling high-temperature exhaust gas discharged from an incinerator, a heat exchanger for generating heated air from the exhaust gas from the cooling device, a reaction tower for neutralizing an acidic component in the exhaust gas, A bag filter provided on the downstream side of the reaction tower, a denitrification device for reducing and denitrifying the exhaust gas from the bag filter, a heat exchange for heating the exhaust gas with the heated air arranged between the bag filter and the denitrification device. The present invention relates to a refuse incineration plant having a furnace and a mixer for mixing the exhaust gas from the denitration device and the heated air.
この発明は、上記のように構成されているので、次のよ
うに作用する。即ち、この焼却炉から排出された排ガス
は、冷却装置、白煙防止用熱交換器を経て冷却され、更
に、反応塔で中和反応されてバグフィルタに導入され
る。Since the present invention is configured as described above, it operates as follows. That is, the exhaust gas discharged from this incinerator is cooled through a cooling device and a white smoke prevention heat exchanger, and is further neutralized in a reaction tower and introduced into a bag filter.
該バグフィルタに導入される時には、排ガスの温度はか
なり低下（１８０℃以下）しているので、ダイオキシン
の発生が抑制され、また、水銀も気化状態になっていな
いので、バグフィルタで煤塵や酸性成分の有害物質と共
に除去される。When it is introduced into the bag filter, the temperature of the exhaust gas is considerably lowered (180 ° C or lower), so that the generation of dioxins is suppressed, and since mercury is not vaporized, dust and acid are not collected by the bag filter. It is removed along with harmful substances.
そして、バグフィルタと脱走装置との間に設けた排ガス
昇温用熱交換器の働きで、排ガスは所定温度まで上昇
し、脱硝装置へと送り込まれる。従って、脱硝装置の触
媒の活性が高められ、脱硝率は高くなる。The exhaust gas is heated to a predetermined temperature by the function of the exhaust gas temperature raising heat exchanger provided between the bag filter and the desorption device, and is sent to the denitration device. Therefore, the activity of the catalyst of the denitration device is increased and the denitration rate is increased.
一方、排ガス昇温用熱交換器で排ガスに熱量を与えた白
煙防止用加熱空気は混合器へ送られ、脱硝装置から送ら
れてきた排ガスと混合される。そして、排ガスは温度が
上昇し、排ガス中の水分率が低下するため、その排ガス
を煙突から大気へ放出した際に白煙が発生しない。On the other hand, the heated air for preventing white smoke, which has given heat to the exhaust gas in the exhaust gas temperature raising heat exchanger, is sent to the mixer and mixed with the exhaust gas sent from the denitration device. Then, since the temperature of the exhaust gas rises and the water content in the exhaust gas decreases, white smoke is not generated when the exhaust gas is discharged from the chimney to the atmosphere.
以下、図面を参照して、この発明によるごみ焼却プラン
トの実施例について説明する。Embodiments of a refuse incineration plant according to the present invention will be described below with reference to the drawings.
第１図はこの発明によるごみ焼却プラントの一実施例を
示す概略図である。FIG. 1 is a schematic diagram showing an embodiment of a refuse incineration plant according to the present invention.
第１図に示すように、この発明によるごみ焼却プラント
は、焼却炉１、冷却装置２、白煙防止用熱交換器３、燃
焼空気用熱交換器４、反応塔５、バグフィルタ６、排ガ
ス昇温用熱交換器７、脱硝装置８、誘引送風機９、混合
器１０、煙突１１などから構成される。As shown in FIG. 1, the waste incineration plant according to the present invention includes an incinerator 1, a cooling device 2, a white smoke prevention heat exchanger 3, a combustion air heat exchanger 4, a reaction tower 5, a bag filter 6, and an exhaust gas. The temperature raising heat exchanger 7, the denitration device 8, the induced air blower 9, the mixer 10, the chimney 11 and the like are included.
焼却炉１は乾燥ストーカ、燃焼ストーカ、後燃焼ストー
カを有するストーカ式の焼却炉１である。The incinerator 1 is a stoker type incinerator 1 having a dry stoker, a combustion stoker, and a post-combustion stoker.
冷却装置２は、焼却炉１でごみを燃焼する時に発生する
排ガスを冷却する装置である。焼却炉１から排出される
排ガスは非常に高温（７５０℃〜９５０℃）になってい
るので、バグフィルタ６の濾布を高温による損傷から守
るために、排ガスは一旦、冷却装置２に導入されて冷却
される。The cooling device 2 is a device that cools the exhaust gas generated when burning the refuse in the incinerator 1. Since the exhaust gas discharged from the incinerator 1 has a very high temperature (750 ° C to 950 ° C), the exhaust gas is once introduced into the cooling device 2 in order to protect the filter cloth of the bag filter 6 from damage due to high temperature. Be cooled.
冷却装置２としては、水噴射ノズルから水を噴射するこ
とにより排ガスを冷却する、いわゆる、水噴射式ガス冷
却装置２が一般に使用されている。なお、ガス冷却装置
２の代わりに廃熱ボイラーを使用して冷却してもよく、
その場合には、排ガスは廃熱ボイラーに直接誘導され
て、水と熱交換することにより冷却される。As the cooling device 2, a so-called water injection type gas cooling device 2 which cools exhaust gas by injecting water from a water injection nozzle is generally used. In addition, you may cool using a waste heat boiler instead of the gas cooling device 2,
In that case, the exhaust gas is directly guided to the waste heat boiler and cooled by exchanging heat with water.
白煙防止用熱交換器３は、白煙防止用送風機１２から送
風された空気を排ガスで熱交換する。熱量を得た加熱空
気は排ガス昇温用熱交換器７に送り込まれる。The white smoke prevention heat exchanger 3 exchanges heat of the air blown from the white smoke prevention blower 12 with exhaust gas. The heated air having obtained the amount of heat is sent to the exhaust gas temperature raising heat exchanger 7.
燃焼空気用熱交換器４は、燃焼用押込送風機１３から送
風された空気を排ガスで熱交換する。熱量を得た加熱空
気は焼却炉１に送られて、焼却炉１における燃焼効率を
向上させるために利用される。The heat exchanger 4 for combustion air exchanges the air blown from the forced air blower 13 for combustion with exhaust gas. The heated air that has obtained the amount of heat is sent to the incinerator 1 and is used to improve the combustion efficiency in the incinerator 1.
これらの白煙防止用熱交換器３及び燃焼空気用熱交換器
４によって、排ガスは更に冷却される。The exhaust gas is further cooled by the white smoke prevention heat exchanger 3 and the combustion air heat exchanger 4.
反応塔５は、消石灰〔Ｃａ（ＯＨ）２〕粉末を相当量噴
霧して、排ガス中の酸性成分である塩化水素、硫黄酸化
物を酸アルカリの固−気反応により中和する装置であ
る。The reaction tower 5 is an apparatus that sprays a considerable amount of slaked lime [Ca (OH) 2 ] powder to neutralize the hydrogen chloride and sulfur oxides, which are the acidic components in the exhaust gas, by the solid-gas reaction of the acid-alkali.
バグフィルタ６は、反応塔５内で中和した後の反応生成
物（ＣａＣｌ２，ＣａＳＯ４）、煤塵などを、内蔵され
た濾布の表面によって捕捉する装置である。バグフィル
タ６に導入される排ガスの温度を約１２０〜１８０℃に
制御するために、バグフィルタ６の前方には温度検出器
が設けられていて、検出した排ガス温度を設定温度と比
較することによりガス冷却装置２の水噴射量調節バルブ
を操作して、水噴射ノズルより噴射される水の量を制御
している。このように、バグフィルタ６における排ガス
の温度は低く維持されているので、サブミクロンの微粒
子に濃縮しているダイオキシン類や水銀等の重金属類も
このバグフィルタ６で除去することができる。The bag filter 6 is a device that traps reaction products (CaCl 2 , CaSO 4 ), soot and the like, which have been neutralized in the reaction tower 5, by the surface of the filter cloth contained therein. In order to control the temperature of the exhaust gas introduced into the bag filter 6 to about 120 to 180 ° C., a temperature detector is provided in front of the bag filter 6, and the detected exhaust gas temperature is compared with the set temperature. The water injection amount control valve of the gas cooling device 2 is operated to control the amount of water injected from the water injection nozzle. As described above, since the temperature of the exhaust gas in the bag filter 6 is kept low, the bag filter 6 can also remove heavy metals such as dioxin and mercury concentrated in submicron particles.
なお、この温度は、バグフィルタ６の濾布材として使用
されるガラス繊維の耐熱温度（２５０〜２８０℃）をか
なり下回るので、濾布の寿命を長くすることができる。Since this temperature is considerably lower than the heat resistant temperature (250 to 280 ° C.) of the glass fiber used as the filter cloth material of the bag filter 6, the life of the filter cloth can be extended.
排ガス昇温用熱交換器７は、白煙防止用熱交換器３から
導入された加熱空気（３００〜３５０℃）によって、バ
グフィルタ６から導入された排ガスの温度を所定温度、
例えば、１９０〜２２０℃まで上昇させる装置である。
排ガスの温度が上昇するのに対し、加熱空気は２２０〜
２５０℃に下がる。The exhaust gas temperature increasing heat exchanger 7 uses the heated air (300 to 350 ° C.) introduced from the white smoke prevention heat exchanger 3 to change the temperature of the exhaust gas introduced from the bag filter 6 to a predetermined temperature,
For example, a device that raises the temperature to 190 to 220 ° C.
Exhaust gas temperature rises, while heated air is 220 ~
The temperature drops to 250 ° C.
脱硝装置８は窒素酸化物を除去する装置である。排ガス
は、脱硝装置８へ導入される前に脱硝装置８の入口で、
アンモニアガスがＮＨ３／ＮＯＸで 0.4〜1.2 程度のモ
ル比で噴霧される。The denitration device 8 is a device that removes nitrogen oxides. The exhaust gas is introduced at the entrance of the denitration device 8 before being introduced into the denitration device 8.
Ammonia gas is sprayed with NH 3 / NO X at a molar ratio of about 0.4 to 1.2.
アンモニアガスを伴う排ガスは、脱硝装置８の脱硝触媒
に接触し、窒素酸化物の濃度は低減される。窒素酸化物
の濃度が低減される割合、即ち、脱硝率は、排ガスの温
度が白煙防止用熱交換器３から導入された加熱空気によ
って１９０〜２２０℃に上昇しているので、約８０％と
いう高率を得ることができる。The exhaust gas accompanied by the ammonia gas contacts the denitration catalyst of the denitration device 8, and the concentration of nitrogen oxides is reduced. The rate at which the concentration of nitrogen oxides is reduced, that is, the denitration rate, is approximately 80% because the temperature of the exhaust gas is raised to 190 to 220 ° C by the heated air introduced from the white smoke prevention heat exchanger 3. You can get a high rate.
誘引送風機９は、燃焼熱から得た蒸気でタービン駆動さ
れ、バグフィルタ６及び脱硝装置８で清浄化されたクリ
ーンガスを吸引して混合器１０へ送り出す。The induction blower 9 is turbine-driven by the steam obtained from the combustion heat, sucks the clean gas cleaned by the bag filter 6 and the denitration device 8, and sends it to the mixer 10.
混合器１０は、脱硝装置８から導入されたクリーンガス
と排ガス昇温用熱交換器７から導入された加熱空気を混
合する。The mixer 10 mixes the clean gas introduced from the denitration device 8 and the heated air introduced from the exhaust gas temperature raising heat exchanger 7.
煙突１１は、混合されたガスを大気へ放出する。The chimney 11 releases the mixed gas to the atmosphere.
次に、このごみ焼却プラントにおける処理フローについ
て説明する。Next, a processing flow in this refuse incineration plant will be described.
焼却炉１から排出された排ガスは、ガス冷却装置２で冷
却され、更に白煙防止用熱交換器３及び燃焼空気用熱交
換器４を通過する際に熱交換によって冷却されて反応塔
５へ送られる。反応塔５内ではアルカリ吸収剤が噴霧さ
れ、排ガス中の酸性成分である塩化水素、硫黄酸化物を
酸アルカリの固−気反応により中和する。この反応の過
程で排ガス温度は目的温度（１２０〜１８０℃）まで低
下する。その後、排ガスがバグフィルタ６を通過するこ
とにより、排ガス中の煤塵、塩化水素、硫黄酸化物が除
去されると共に、水銀も除去され、且つダイオキシンの
生成抑制と除去が行われる。清浄化された排ガス（熱量
ＱＧ）は、下流側の脱硝装置８に導入される前に、排ガ
ス昇温用熱交換器７で白煙防止用加熱空気（熱量Ｑ）か
ら熱量（Ｑ１）を得て、温度が上昇する（１９０〜２２
０℃）。このため、排ガス昇温用熱交換器７を通過した
後の排ガスの熱量は（ＱＧ＋Ｑ１）となり、一方、白煙
防止用加熱空気の熱量は（Ｑ−Ｑ１）となる。脱硝装置
８で窒素酸化物を分解した後に、排ガス（熱量ＱＧ＋Ｑ
１）は、排ガス昇温用熱交換器７で熱を奪われた白煙防
止用加熱空気（熱量Ｑ−Ｑ１）と一緒に混合器１０に混
入され、煙突１１から排出される。その時の排出熱量
は、 （ＱＧ＋Ｑ１）＋（Ｑ−Ｑ１）＝ＱＧ＋Ｑ となる。The exhaust gas discharged from the incinerator 1 is cooled by the gas cooling device 2 and further cooled by heat exchange when passing through the white smoke prevention heat exchanger 3 and the combustion air heat exchanger 4 to the reaction tower 5. Sent. In the reaction tower 5, the alkali absorbent is sprayed, and the hydrogen chloride and the sulfur oxide which are the acidic components in the exhaust gas are neutralized by the solid-gas reaction of the acid-alkali. In the course of this reaction, the exhaust gas temperature drops to the target temperature (120 to 180 ° C). After that, when the exhaust gas passes through the bag filter 6, the soot dust, hydrogen chloride, and sulfur oxides in the exhaust gas are removed, mercury is also removed, and dioxins are suppressed and removed. Before being introduced into the NOx removal device 8 on the downstream side, the purified exhaust gas (heat quantity Q G ) is heated from the white smoke prevention heating air (heat quantity Q) to the heat quantity (Q 1 ) in the exhaust gas temperature raising heat exchanger 7. And the temperature rises (190-22
0 ° C). Therefore, the heat quantity of the exhaust gas after passing through the exhaust gas temperature raising heat exchanger 7 becomes (Q G + Q 1 ), while the heat quantity of the white smoke prevention heated air becomes (Q-Q 1 ). After decomposing nitrogen oxides with the denitration device 8, exhaust gas (heat quantity Q G + Q
1 ) is mixed with the white smoke prevention heated air (heat quantity Q-Q 1 ) deprived of heat by the exhaust gas temperature raising heat exchanger 7 in the mixer 10 and discharged from the chimney 11. The amount of heat exhausted at that time is (Q G + Q 1 ) + (Q−Q 1 ) = Q G + Q.
この熱量は、排ガス昇温用熱交換器７を設けない従来の
場合の排出熱量（ＱＧ＋Ｑ）と同一熱量である。This amount of heat is the same as the amount of heat exhausted (Q G + Q) in the conventional case where the exhaust gas temperature raising heat exchanger 7 is not provided.
従って、大気中に放出される熱量の大きさは従来と変わ
らない。Therefore, the amount of heat released into the atmosphere is the same as in the conventional case.
次に、白煙発生防止の原理について説明する。Next, the principle of preventing white smoke generation will be described.
第２図は、温度と該温度における空気又は排ガス中に含
まれる水分との関係を示すグラフである。FIG. 2 is a graph showing the relationship between the temperature and the moisture contained in the air or the exhaust gas at the temperature.
Ａ点はバグフィルタ６通過後の排ガスの状態、Ｂ点は排
ガス昇温用熱交換器７で加熱された排ガスの状態、Ｃ点
は排ガス昇温用熱交換器７通過後の白煙防止用加熱空気
の状態、Ｄ点は混合器１０で白煙防止用加熱空気が混入
された排ガスの状態、Ｅ点は大気の状態である。The point A is the state of the exhaust gas after passing through the bag filter 6, the point B is the state of the exhaust gas heated by the exhaust gas temperature increasing heat exchanger 7, and the point C is for preventing white smoke after passing through the exhaust gas temperature increasing heat exchanger 7. The state of the heated air, the point D is the state of the exhaust gas in which the white smoke preventing heated air is mixed in the mixer 10, and the point E is the state of the atmosphere.
また、曲線Ｆは飽和水蒸気曲線Ｆを表している。Further, the curve F represents the saturated water vapor curve F.
仮に、バグフィルタ６の通過後の排ガス（Ａ点）を煙突
１１から大気（Ｅ点）中に放出するとすれば、放出直後
の排ガスはＡ点とＥ点を結ぶ直線上の点の状態になる。
Ａ点とＥ点を結ぶ直線は、飽和水蒸気曲線と２点で交わ
るため、放出直後の排ガスの状態がこの２点間にある場
合には白煙が発生する。If the exhaust gas (point A) after passing through the bag filter 6 is to be discharged from the chimney 11 into the atmosphere (point E), the exhaust gas immediately after being discharged will be in a state of a point on a straight line connecting points A and E. .
Since the straight line connecting the points A and E intersects with the saturated water vapor curve at two points, white smoke is generated when the state of the exhaust gas immediately after discharge is between these two points.
このように、Ｅ点とを結ぶ直線が飽和水蒸気曲線Ｆと２
点で交わるような状態の排ガスを大気中に放出すれば、
白煙が発生する。Thus, the straight line connecting the point E is the saturated water vapor curve F and 2
If exhaust gas in the state where it intersects at the point is released into the atmosphere,
White smoke is generated.
ところが、この発明におけるごみ焼却プラントは、排ガ
ス昇温用熱交換器７で加熱された白煙防止用加熱空気
（Ｃ点）と排ガス昇温用熱交換器７通過後の排ガス（Ｂ
点）を混合器１０で混合して、混合した排ガス（Ｄ点）
を大気（Ｅ点）中へ放出するようにしているので、グラ
フから明らかなように、Ｄ点とＥ点を結ぶ直線は飽和水
蒸気曲線Ｆと交わらない。従って、大気中に排ガスを放
出しても白煙を発生しない。However, in the refuse incineration plant according to the present invention, the white smoke preventing heated air (point C) heated by the exhaust gas temperature raising heat exchanger 7 and the exhaust gas (B
Point) is mixed in the mixer 10 and mixed exhaust gas (point D)
Is emitted into the atmosphere (point E), the straight line connecting points D and E does not intersect the saturated water vapor curve F, as is apparent from the graph. Therefore, white smoke is not generated even if exhaust gas is discharged into the atmosphere.
このように、排ガスに加熱空気を混入して、排ガスの温
度を上昇させると共に、水分含有率を低く抑えることに
より、グラフにおいてＤ点を右側かつ下側に移動させる
ことにより、Ｅ点とＤ点を結ぶ直線が飽和水蒸気曲線Ｆ
に交わらないようにすれば、白煙を防止することができ
る。In this way, by mixing heated air into the exhaust gas to raise the temperature of the exhaust gas and keep the moisture content low, by moving point D to the right and downward in the graph, points E and D can be obtained. The straight line connecting the lines is the saturated steam curve F
You can prevent white smoke if you do not intersect with.
〔発明の効果〕 この発明によるごみ焼却プラントは、上記のように構成
されているので、次のような効果を有する。[Effects of the Invention] Since the refuse incineration plant according to the present invention is configured as described above, it has the following effects.
白煙防止用の加熱空気の熱量を２工程即ち排ガス昇温用
熱交換器と混合器の２つに分けて排ガスに与えることが
でき、バグフィルタの下流に配置した熱交換器によって
排ガス量を変化させることなく、熱量だけを排ガスに与
えるので、脱硝装置における温度を高くすることができ
る。従って、脱硝装置の触媒の活性が高められ、高い脱
硝率を得ることができる。The heat quantity of the heated air for preventing white smoke can be given to the exhaust gas in two steps, that is, the exhaust gas temperature raising heat exchanger and the mixer, and the exhaust gas quantity can be changed by the heat exchanger arranged downstream of the bag filter. Since only the amount of heat is given to the exhaust gas without changing, the temperature in the denitration device can be increased. Therefore, the activity of the catalyst of the denitration device is enhanced, and a high denitration rate can be obtained.
また、脱硝装置に導入する直前で排ガスの温度を上昇さ
せるので、その前段階のバグフィルタでの温度は１８０
℃以下というかなり低い温度に抑えることができる。こ
のため、ダイオキシンの生成を抑制し、水銀を捕捉する
ことができるだけでなく、バグフィルタの濾布の耐熱温
度よりも排ガスの温度がかなり低いので、濾布の寿命を
長くすることができる。Moreover, since the temperature of the exhaust gas is raised immediately before introduction into the denitration device, the temperature in the bag filter at the previous stage is 180
It can be suppressed to a considerably low temperature of ℃ or less. For this reason, not only can dioxin formation be suppressed and mercury can be captured, but the temperature of the exhaust gas is considerably lower than the heat resistant temperature of the filter cloth of the bag filter, so that the life of the filter cloth can be extended.
更に、脱硝装置から送られてきた清浄化された排ガス
は、混合器で白煙防止用加熱空気を混入した上で煙突か
ら大気へ放出されるので、排ガスの温度は上昇し、かつ
排ガス中の水分の含有率の低下が図られ、白煙の発生を
防止することができる。Furthermore, the purified exhaust gas sent from the denitration device mixes with the white smoke prevention heated air in the mixer and is then released from the chimney to the atmosphere, so the temperature of the exhaust gas rises and the exhaust gas The water content can be reduced, and white smoke can be prevented from being generated.
第１図はこの発明によるごみ焼却プラントの一実施例を
示す概略図、第２図は温度と該温度における空気又は排
ガス中に含まれる水分との関係を示すグラフ、及び第３
図は従来のごみ焼却プラントを示す概略図である。 １……焼却炉、２……ガス冷却装置、３……白煙防止用
熱交換器、４……燃焼空気用熱交換器、５……反応塔、
６……バグフィルタ、７……排ガス昇温用熱交換器、８
……脱硝装置、９……誘引送風機、１０……混合器、１
１……煙突、１２……白煙防止用送風機、１３……燃焼
用押込送風機。FIG. 1 is a schematic diagram showing an embodiment of a refuse incineration plant according to the present invention, FIG. 2 is a graph showing a relationship between temperature and moisture contained in air or exhaust gas at the temperature, and FIG.
The figure is a schematic view showing a conventional refuse incineration plant. 1 ... incinerator, 2 ... gas cooling device, 3 ... white smoke prevention heat exchanger, 4 ... combustion air heat exchanger, 5 ... reaction tower,
6 ... Bag filter, 7 ... Exhaust gas temperature raising heat exchanger, 8
...... Denitration equipment, 9 ...... Induction blower, 10 ...... Mixer, 1
1 ... Chimney, 12 ... White smoke prevention blower, 13 ... Combustion push blower.
Claims (1)
する冷却装置、該冷却装置からの排ガスで加熱空気を発
生させる熱交換器、排ガス中の酸性成分を中和反応させ
る反応塔、該反応塔の下流側に設けたバグフィルタ、該
バグフィルタからの排ガスを還元脱硝する脱硝装置、前
記バグフィルタと前記脱硝装置との間に配置した前記加
熱空気で前記排ガスを昇温する熱交換器、及び前記脱硝
装置からの排ガスと前記加熱空気とを混合する混合器、
を有するごみ焼却プラント。1. A cooling device for cooling high-temperature exhaust gas discharged from an incinerator, a heat exchanger for generating heated air by the exhaust gas from the cooling device, a reaction tower for neutralizing an acidic component in the exhaust gas, A bag filter provided on the downstream side of the reaction tower, a denitrification device for reducing and denitrifying exhaust gas from the bag filter, and a heat exchanger for heating the exhaust gas with the heated air arranged between the bag filter and the denitrification device. And a mixer for mixing the exhaust gas from the denitration device with the heated air,
Waste incineration plant with.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000990A JPH0635888B2 (en) | 1990-01-09 | 1990-01-09 | Garbage incineration plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000990A JPH0635888B2 (en) | 1990-01-09 | 1990-01-09 | Garbage incineration plant |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH03207908A JPH03207908A (en) | 1991-09-11 |
| JPH0635888B2 true JPH0635888B2 (en) | 1994-05-11 |
Family
ID=11489037
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2000990A Expired - Lifetime JPH0635888B2 (en) | 1990-01-09 | 1990-01-09 | Garbage incineration plant |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0635888B2 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2702662B2 (en) * | 1993-09-30 | 1998-01-21 | 日本碍子株式会社 | Combustion exhaust gas treatment apparatus and treatment method |
| JP2786598B2 (en) * | 1994-07-07 | 1998-08-13 | 株式会社プランテック | Air heater for white smoke prevention |
| JP4647960B2 (en) * | 2004-09-10 | 2011-03-09 | バブコック日立株式会社 | Glass melting furnace exhaust gas treatment method and treatment apparatus |
| JP5279062B2 (en) * | 2007-02-21 | 2013-09-04 | 株式会社タクマ | Combustion exhaust gas treatment method and combustion exhaust gas treatment apparatus |
| JP6678265B1 (en) * | 2019-02-28 | 2020-04-08 | 月島機械株式会社 | Apparatus and method for treating flue gas |
-
1990
- 1990-01-09 JP JP2000990A patent/JPH0635888B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH03207908A (en) | 1991-09-11 |
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