JPH03207908A - Refuse incinerator - Google Patents
Refuse incineratorInfo
- Publication number
- JPH03207908A JPH03207908A JP90990A JP99090A JPH03207908A JP H03207908 A JPH03207908 A JP H03207908A JP 90990 A JP90990 A JP 90990A JP 99090 A JP99090 A JP 99090A JP H03207908 A JPH03207908 A JP H03207908A
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- temperature
- heat exchanger
- bag filter
- white smoke
- 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.)
- Granted
Links
- 238000002156 mixing Methods 0.000 claims abstract description 3
- 238000001816 cooling Methods 0.000 claims description 19
- 238000006243 chemical reaction Methods 0.000 claims description 18
- 238000004056 waste incineration Methods 0.000 claims description 15
- 230000002378 acidificating effect Effects 0.000 claims description 6
- 239000007789 gas Substances 0.000 abstract description 122
- 239000000779 smoke Substances 0.000 abstract description 40
- 230000002265 prevention Effects 0.000 abstract description 22
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 abstract description 12
- 229910052753 mercury Inorganic materials 0.000 abstract description 12
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 abstract description 7
- 238000010438 heat treatment Methods 0.000 abstract description 7
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 abstract description 7
- 229910000041 hydrogen chloride Inorganic materials 0.000 abstract description 7
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 abstract description 5
- 229910052815 sulfur oxide Inorganic materials 0.000 abstract description 4
- 238000000034 method Methods 0.000 abstract description 3
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 abstract 2
- 239000006096 absorbing agent Substances 0.000 abstract 1
- 150000002731 mercury compounds Chemical class 0.000 abstract 1
- 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 Chemical class O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 239000000428 dust Substances 0.000 description 8
- 230000007423 decrease Effects 0.000 description 7
- 150000002013 dioxins Chemical class 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 239000004744 fabric Substances 0.000 description 6
- 230000001965 increasing effect Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000004071 soot Substances 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 239000003513 alkali Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000002829 reductive effect Effects 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 239000002699 waste material Substances 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
- 230000033228 biological regulation Effects 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
- 239000012717 electrostatic precipitator Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 230000031018 biological processes and functions Effects 0.000 description 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000003028 elevating effect Effects 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 230000030279 gene silencing Effects 0.000 description 1
- 239000003365 glass fiber Substances 0.000 description 1
- 239000000383 hazardous chemical Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Abstract
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儂えたごみ焼却プラ
ントに関する．
〔従来の技術〕
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（ＨＣＩ）、硫黄酸化物（Ｓｏ．）、窒素酸化物
（Ｎｏ）１ ３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。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] This invention relates to a waste incineration plant equipped with an exhaust gas treatment device for treating exhaust gas discharged from an incinerator such as a municipal waste incinerator. [Prior Art] In recent years, incineration has become the mainstream for municipal waste treatment. The exhaust gas emitted from incineration contains large amounts of harmful substances such as soot and dust, hydrogen chloride (HCI), sulfur oxides (So.), and nitrogen oxides (No. 13).
In order to prevent the occurrence of secondary pollution caused by waste incineration, there is a need to develop exhaust gas treatment equipment that can efficiently and effectively remove these substances. Emission concentrations are 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。2. Description of the Related Art Conventionally, as a waste incineration plant equipped with an exhaust gas treatment device for treating exhaust gas discharged from a municipal waste incinerator, 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
Ｗ２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
ガス中の酸性威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１３０，該集ｍ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から構或されている。This waste incineration plant consists of an incinerator 1, a cooling device 2 that cools the high-temperature exhaust gas discharged from the incinerator 1, and a cooling device W2 that exchanges heat with the exhaust gas introduced from the cooling device W2 and discharges heated air for preventing white smoke. A heat exchanger 3 for preventing white smoke, a reaction tower 5 that neutralizes acidic components in the heat-exchanged exhaust gas, a dust collector 130 provided on the downstream side of the reaction tower 5, and a dust collector 30. The denitrification device 8 reduces and denitrates the exhaust gas, and the mixer 10 mixes the exhaust gas introduced from the denitrification device 8 with 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 combustion air heat exchanger 4 is provided between the white smoke prevention heat exchanger 3 and the dust collector 30. Furthermore, a denitrification device 8
An induced blower 9 sucks exhaust gas from the air and sends it to the mixer 10
, a chimney 11 for releasing 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．
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戒分の有害物質は中和反応を起こし
、その反応生戒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ＮＨ
，ガスを噴霧し、その下ｉ！ｉ？Ｌ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ＩＩ
ＩＩ９で吸引されて混合器１０へと送られる。混合器１
０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 processing flow of this waste incineration plant is as follows. High-temperature exhaust gas discharged from the incinerator 1 is cooled by a cooling device 2, and further heat exchanged by a white smoke prevention heat exchanger 3 and a combustion air heat exchanger 4. Next, an alkaline agent such as slaked lime is sprayed in the reaction tower 5, and acidic harmful substances such as hydrogen chloride contained in the exhaust gas undergo a neutralization reaction, and the reaction substances are collected by electrostatic precipitate. When passing through a dust collector 30 such as a container, the dust is removed together with soot and dust. After that, NH in the flue
, Spray the gas and then i! i? Reductive denitrification is performed in the denitrification device 8 installed on the L side. As a result, nitrogen oxides are removed from the exhaust gas, and the purified exhaust gas is transferred to the induced draft II.
It is sucked in by II9 and sent to mixer 10. mixer 1
0, the white smoke prevention heated air obtained by the white smoke prevention heat exchanger 3 is mixed with the purified exhaust gas to increase the temperature of the exhaust gas. In this way, the purified exhaust gas is once heated and then released into the atmosphere from the chimney 11.
Efforts are being made to prevent 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．ダイオキシンの生戒過程は明確に
は解明されていないが、３００℃前後の温度で電気集塵
器３０内で場威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で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 hazardous substances have been becoming increasingly strict in recent years, and it is expected that substances such as dioxins and mercury will also become subject to these regulations. Although the biological process of dioxin has not been clearly elucidated, it has been confirmed that it is present in the electrostatic precipitator 30 at a temperature of around 300°C. Additionally, mercury is in a vaporized state at a temperature of 300° C., and therefore cannot be captured by the electrostatic precipitator 30 at present.
そこで、ダイオキシンの生或を抑制し、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｝足することのできるバグフィル
タを集！Ｉ器として採用することが考えられる。Therefore, in order to suppress the production and condensation of dioxin and to avoid vaporization of mercury, the temperature of the exhaust gas is lowered (180°C), and in order to remove mercury, the mercury particles attached to fine particles are captured. A collection of bug filters that can be used! It is conceivable to adopt it as an I-device.
しかしながら、排ガスの温度が低下すると、脱硝装置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。However, when the temperature of the exhaust gas decreases, the denitrification device 8
Since the activity of the denitrification catalyst decreases, there is a problem that the denitrification efficiency decreases significantly.
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１
８５℃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を通遇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Ｈ３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。For example, when the exhaust gas temperature is between 210°C and 220°C, the denitrification rate is approximately 80%, whereas when the exhaust gas temperature is approximately 1.
The denitrification rate at 85°C drops to about 65%. On the other hand, when the temperature of the exhaust gas flowing through the denitrification device 8 decreases, even if the temperature of the exhaust gas is increased in the downstream mixer 10 using the high-temperature heated air obtained from the white smoke prevention heat exchange H3, the exhaust gas remains in the exhaust gas. cannot keep the moisture content low.
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．
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ｉ！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．
（ｆｆｌａを解決するための手段〕
この発明は、上記目的を達或するため、次のように構威
されている．
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、排ガス中の酸性戒分を中和反
咬させる反応塔、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間する．〔作用〕
この発明は、上記のように構或されているので、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
。Therefore, when the exhaust gas is released into the atmosphere, it reaches saturated water vapor and generates a large amount of water vapor, that is, white smoke, which is a problem. Therefore, in order to remove dioxins and mercury and prevent a decrease in denitrification efficiency and the generation of white smoke, the temperature of the exhaust gas should be adjusted using the bag filter i! By solving the problem of having a low nitrification level at the time of denitrification and a high level when introduced into the denitrification equipment, we can improve the denitrification efficiency and prevent the generation of white smoke, as well as provide a waste incineration plant that can remove dioxins and mercury. be. (Means for solving ffla) In order to achieve the above object, the present invention is structured as follows. That is, the present invention provides a cooling method for cooling high-temperature exhaust gas discharged from an incinerator. A device, a heat exchanger that generates heated air with exhaust gas from the cooling device, a reaction tower that neutralizes acidic substances in the exhaust gas, a bag filter provided on the downstream side of the reaction tower, and exhaust gas from the bag filter. a denitrification device that reduces and denitrates the denitrification device; a heat exchanger that raises the temperature of the exhaust gas with the heated air disposed between the bag filter and the denitrification device; and a mixer that mixes the exhaust gas from the denitrification device and the heated air. [Operation] Since the present invention is constructed as described above, it operates as follows. That is, the exhaust gas discharged from this incinerator is It is cooled through a white smoke prevention heat exchanger, then 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或分の有害物質と共
に除去される。By the time the exhaust gas is introduced into the bag filter, the temperature of the exhaust gas has dropped considerably (below 180 degrees Celsius), so the generation of dioxins is suppressed, and mercury is not in a vaporized state, so the bag filter removes soot and acid. It is removed along with some harmful substances.
そして、バグフィルタと脱硝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．
一方、排ガス昇濫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．
〔実施例〕
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。The exhaust gas is then raised to a predetermined temperature by the action of a heat exchanger for raising the temperature of the exhaust gas provided between the bag filter and the denitrification device, and then sent to the denitrification device. Therefore, the activity of the catalyst in the denitration equipment is increased, and the denitrification rate is increased. On the other hand, heated air for white smoke prevention, which has given heat to the exhaust gas in the exhaust gas elevating heat exchanger, is sent to the mixer and mixed with the exhaust gas sent from the denitrification device. As the temperature of the exhaust gas increases and the moisture content in the exhaust gas decreases, no white smoke is generated when the exhaust gas is released into the atmosphere from the chimney. [Example] Hereinafter, an example of a waste incineration plant according to the present invention will be described 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 waste 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ｌ、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１１９、混
合器１０、煙突１１などから構威される．
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．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。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, an exhaust gas It consists of a heating heat exchanger 7, a denitrification device 8, an induced draft 119, a mixer 10, a chimney 11, etc. The incinerator 1 is a stoker-type incinerator 1 having a drying stoker, a combustion stoker, and an after-combustion stoker. The cooling device 2 is a device that cools the exhaust gas generated when garbage is burned 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 first introduced into the cooling device 2 in order to protect the filter cloth of the bag filter 6 from being damaged by the high temperature. and cooled down.
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。As the cooling device 2, a so-called water injection type gas cooling device 2 that cools exhaust gas by injecting water from a water injection nozzle is generally used.
なお、ガス冷却装Ｍ２の代わりにａ熟ボイラーを使用し
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．
白煙防止用熱交換器３は、白煙防止用送ｆｆｌｌ１１１
２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．
燃焼空気用熱交換８４は、燃焼用押込送風機１３から送
凰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．
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．反応塔５は、消
石灰（Ｃａ （ＯＨ）ｔ ）粕末を相当量噴霧して、排
ガス中の酸性或分である塩化水素、硫黄酸化物を酸アル
カリの固一気反応により中和する装置である。Note that an A boiler may be used instead of the gas cooling system M2 for cooling, and in that case, the exhaust gas is directly guided to the waste heat boiler and cooled by exchanging heat with water. The white smoke prevention heat exchanger 3 is the white smoke prevention heat exchanger ffll111.
Heat exchanges the air blown from 2 with exhaust gas. The heated air that has gained heat is sent to the heat exchanger 7 for raising the exhaust gas temperature. The combustion air heat exchanger 84 heat-exchanges the air sent from the combustion forced air blower 13 with exhaust gas. The heated air that has gained heat is sent to the incinerator 1 and used to improve the combustion efficiency in the incinerator 1. The exhaust gas is further cooled by the white smoke prevention heat exchanger 3 and the combustion air heat exchanger 4. The reaction tower 5 is a device that sprays a considerable amount of slaked lime (Ca(OH)t) lees powder to neutralize hydrogen chloride and sulfur oxides, which are acidic components in the exhaust gas, by a solid-at-once reaction of acid and alkali. .
バグフィルタ６は、反応塔５内で中和した後の反応生戒
物（ＣａＣ１ｚ ．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 (CaC1z.CaSO4), soot dust, etc. after being neutralized in the reaction tower 5 using the surface of a built-in filter cloth. The temperature of the exhaust gas introduced into the bag filter 6 is set to about 120 to 180.
℃, a temperature detector is provided in front of the bag filter 6, and by comparing the detected exhaust gas temperature with a set temperature, the water injection amount control valve of the gas cooling device 2 is operated. It controls the amount of water sprayed from the water spray nozzle. In this way, the temperature of the exhaust gas in the bag filter 6 is maintained low, so that heavy metals such as dioxins and mercury that are concentrated in submicron particles can also be removed by the bag filter 6.
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．
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’ｃ）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。In addition, since this temperature is considerably lower than the heat resistance 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. The exhaust gas heating heat exchanger 7 is heated by the heated air (300 to 350'c) introduced from the white smoke prevention heat exchanger 3.
This device raises the temperature of the exhaust gas introduced from the bag filter 6 to a predetermined temperature, for example, 190 to 220°C. While the temperature of the exhaust gas rises, the temperature of the heated air rises to 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ＮＨ，／ＮＯＸで０．４〜１．２程度
のモル比で噴霧される。The denitrification device 8 is a device that removes nitrogen oxides. Before being introduced into the denitrification device 8, the exhaust gas is passed through the inlet of the denitrification device 8,
Ammonia gas is sprayed at a molar ratio of NH,/NOX 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
ζこ接触し、窒素酸化物の濃度はＷ滅さ力，る。窒素酸
化物の濃度が低滅される割合、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 containing ammonia gas comes into contact with the denitrification catalyst ζ of the denitrification device 8, and the concentration of nitrogen oxides is reduced. The rate at which the concentration of nitrogen oxides is reduced, that is, the denitrification rate, is approximately 80°C 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.
% can be obtained.
誘引送風機９は、燃焼熱から得た蕉気でタービン駆動さ
れ、バグフィルタ５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 induced blower 9 is driven by a turbine using air obtained from combustion heat, sucks clean gas purified by the bag filter 5 and the denitrification 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
と排ガス昇温用執交換器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 denitrification device 8 and the heated air introduced from the exhaust gas temperature raising exchanger 7.
煙突１１は、混合されたガスを大気へ放出する。Chimney 11 releases the mixed gas to the atmosphere.
次Ｃこ、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, the processing flow in this waste incineration plant will be explained.
焼却炉ｌ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、排ガス中の酸性或分である塩化水素、硫黄酸化物を
酸アルカリの固一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
生或抑制と除去が行われる。The exhaust gas discharged from the incinerator 1 is cooled by a gas cooling device 2, and further cooled by heat exchange as it passes through a white smoke prevention heat exchanger 3 and a combustion air heat exchanger 4, and is then sent to a reaction tower 5. Sent. In the reaction tower 5, an alkali absorbent is sprayed to neutralize hydrogen chloride and sulfur oxide, which are acidic components in the exhaust gas, by a solid reaction of acid and alkali. During the course of this reaction, the exhaust gas temperature decreases to the target temperature (120 to 180°C). After that, the exhaust gas passes through the bag filter 6, so that soot, hydrogen chloride, and sulfur oxides in the exhaust gas are removed, mercury is also removed, and the production or suppression of dioxins is suppressed and removed.
清浄化された排ガス（凱量Ｑ，）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）から艶量（Ｑ，）を得て、温度
が上昇する（１９０〜２２０℃〉。このため、排ガス昇
温用軌交換器７を通過した後の排ガスの熱量は（ＱＧ”
Ｑｌ ）となり、一方、白煙防止用加熱空気の熱量は（
Ｑ−Ｑ，）となる．脱硝装Ｗ８で窒素酸化物を分解した
後に、排ガス（熱量ＱＧ 十〇ｌ ）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
−Ｑ．）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 ＋Ｑ，）＋
（Ｑ−Ｑｌ ）＝ＱＧ ＋Ｑとなる。The purified exhaust gas (heat amount Q,) is converted into gloss amount (Q, ,), and the temperature rises (190 to 220°C>. Therefore, the amount of heat of the exhaust gas after passing through the exhaust gas temperature raising rail exchanger 7 is (QG").
Ql), and on the other hand, the amount of heat of the heated air for white smoke prevention is (
Q-Q, ). After decomposing nitrogen oxides in the denitrification unit W8, the exhaust gas (calorific value QG 100 l) is converted into white smoke prevention heated air (calorific value Q
-Q. ) is mixed into the mixer 10 and discharged from the chimney 11. The amount of heat released at that time is (QG +Q,)+
(Q-Ql)=QG+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（ Ｑ ｒ，↓Ｑ〉と同一熱量である．
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．
次に、白煙発生防止の原理について説明する。This amount of heat is the same as the amount of emitted heat (Q r,↓Q〉) in the conventional case where the heat exchanger 7 for raising the exhaust gas temperature is not installed. Therefore, the amount of heat released into the atmosphere is different from the conventional case. No. Next, the principle of preventing white smoke generation will be explained.
第２図は、塩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 salinity and moisture contained in air or exhaust gas at the temperature.
Ａ点はハグフィルタ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
は排ガス昇温用勢交換器７通３Ｆ４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。Point A is the state of the exhaust gas after passing through the Hag filter 6, point B is the state of the exhaust gas heated by the heat exchanger 7 for heating the exhaust gas, and point C is the state of the exhaust gas after passing through the heat exchanger 7 for heating the exhaust gas, white smoke prevention after 3F4. Point D is the state of the exhaust gas mixed with heated air for white smoke prevention in the mixer 10, and 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。Moreover, 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 after passing through the bag filter 6 (point A) is released from the chimney 11 into the atmosphere (point E), the exhaust gas immediately after being released will be in the state of a point on the straight line connecting points A and E. ．．
Since the straight line connecting points A and E intersects the saturated steam curve at two points, white smoke will be generated if the state of the exhaust gas immediately after release 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。In this way, the straight line connecting point E is the saturated water vapor curve F and 2
If exhaust gases that intersect at a point are 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）と排ガス昇温用艶交換器７ｉｉｌ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
水草気曲線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, the waste incineration plant according to the present invention uses heated air for preventing white smoke (
point C) and the exhaust gas after passing through the exhaust gas temperature increasing gloss exchanger 7iil (
Since the mixture (point B) is mixed in the mixer 10 and the mixed exhaust gas (point D) is released into the atmosphere (point E), as is clear from the graph, the straight line connecting points D and E is does not intersect with the saturated aquatic plants curve F. Therefore, no white smoke is generated even if the exhaust gas is released 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草気曲ｕＦ
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 keeping the moisture content low, point D can be moved to the right and lower side in the graph, and points E and D can be changed. The straight line that connects the saturated water plants and air curve uF
White smoke can be prevented by ensuring that the two do not intersect with each other.
この発明によるごみ焼却プラントは、上記のように構威
されているので、次のような効果を有する。Since the waste 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工程即ち排ガス消音用
熱交換器とボ合器の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＜、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 amount of heat from heated air for white smoke prevention can be divided into two processes: a heat exchanger for exhaust gas silencing and a combiner. Since only the amount of heat is given to the exhaust gas without changing it, the temperature in the denitrification device can be increased. Therefore, the activity of the catalyst in the denitrification device is increased, and a high denitrification 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、ダイオキシンの生或を抑制し、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。In addition, the temperature of the exhaust gas is raised just before it is introduced into the denitrification equipment, so the temperature at the bag filter in the previous stage is 180℃.
The temperature can be kept very low, below ℃. Therefore, not only can the production of dioxins be suppressed and mercury be captured, but also the life of the filter cloth can be extended because the temperature of the exhaust gas is considerably lower than the heat resistance temperature of the filter cloth of the bag filter.
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 denitrification equipment is mixed with heated air to prevent white smoke in the mixer and then released from the chimney into the atmosphere, so the temperature of the exhaust gas increases and the This reduces the moisture content and prevents the generation of white smoke.
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むける空気又は排
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へ−−−一焼却炉、２−−−−ガス冷却装置、３−−
−−−白煙防止用熱交換器、４ −−−−一燃焼空気用
熱交換器、５−−−一反応塔、６−−−−バグフィルタ
、７−−−一排ガス昇温用熱交換器、８−一一一脱硝装
置、９ −−−−−誘弓送風機、１ （１−一一−混合
器、１ １−−−−−一煙突、１２白煙防止用送風機、
１ ３−−−−一燃焼用押込送風機。FIG. 1 is a schematic diagram showing an embodiment of a waste incineration plant according to the present invention, FIG. 2 is a graph showing the relationship between temperature and moisture contained in air or exhaust gas toward the temperature, and FIG.
The figure is a schematic diagram showing a conventional waste incineration plant. To 1---1 incinerator, 2---gas cooling device, 3---
--- Heat exchanger for preventing white smoke, 4 --- Heat exchanger for combustion air, 5 --- Reaction tower, 6 --- Bag filter, 7 --- Heat for raising exhaust gas temperature exchanger, 8-111 denitrification device, 9 ---- bow blower, 1 (1-11- mixer, 1 1----1 chimney, 12 white smoke prevention blower,
1 3 - - Forced blower for combustion.
Claims (1)
、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。A cooling device that cools high-temperature exhaust gas discharged from the incinerator, a heat exchanger that generates heated air with the exhaust gas from the cooling device, a reaction tower that neutralizes acidic components in the exhaust gas, and a downstream side of the reaction tower. a bag filter provided in the bag filter, a denitrification device that reduces and denitrates the exhaust gas from the bag filter, a heat exchanger that raises the temperature of the exhaust gas with the heated air arranged between the bag filter and the denitrification device, and the denitrification device a mixer for mixing the heated air with exhaust gas from the waste incineration plant.
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 true JPH03207908A (en) | 1991-09-11 |
| JPH0635888B2 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) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0796134A (en) * | 1993-09-30 | 1995-04-11 | Ngk Insulators Ltd | Device for treating waste combustion gas and treating method therefor |
| JPH0821617A (en) * | 1994-07-07 | 1996-01-23 | Plantec:Kk | White smoke preventing air heating device |
| JP2006075764A (en) * | 2004-09-10 | 2006-03-23 | Babcock Hitachi Kk | Glass melting furnace-exhaust gas treatment method and treatment apparatus |
| JP2008200631A (en) * | 2007-02-21 | 2008-09-04 | Takuma Co Ltd | Method and apparatus for treating combustion exhaust gas |
| WO2020174730A1 (en) * | 2019-02-28 | 2020-09-03 | 月島機械株式会社 | Apparatus and method for treating combustion exhaust gas |
-
1990
- 1990-01-09 JP JP2000990A patent/JPH0635888B2/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0796134A (en) * | 1993-09-30 | 1995-04-11 | Ngk Insulators Ltd | Device for treating waste combustion gas and treating method therefor |
| JPH0821617A (en) * | 1994-07-07 | 1996-01-23 | Plantec:Kk | White smoke preventing air heating device |
| JP2006075764A (en) * | 2004-09-10 | 2006-03-23 | Babcock Hitachi Kk | Glass melting furnace-exhaust gas treatment method and treatment apparatus |
| 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 |
| JP2008200631A (en) * | 2007-02-21 | 2008-09-04 | Takuma Co Ltd | Method and apparatus for treating combustion exhaust gas |
| WO2020174730A1 (en) * | 2019-02-28 | 2020-09-03 | 月島機械株式会社 | Apparatus and method for treating combustion exhaust gas |
| JP2020139696A (en) * | 2019-02-28 | 2020-09-03 | 月島機械株式会社 | Device and method of processing combustion exhaust |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0635888B2 (en) | 1994-05-11 |
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