JPH02265618A - Capture of sulfur trioxide in waste gas - Google Patents
Capture of sulfur trioxide in waste gasInfo
- Publication number
- JPH02265618A JPH02265618A JP1086845A JP8684589A JPH02265618A JP H02265618 A JPH02265618 A JP H02265618A JP 1086845 A JP1086845 A JP 1086845A JP 8684589 A JP8684589 A JP 8684589A JP H02265618 A JPH02265618 A JP H02265618A
- Authority
- JP
- Japan
- Prior art keywords
- amount
- exhaust gas
- waste gas
- electrostatic precipitator
- injected
- 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.)
- Pending
Links
- 239000002912 waste gas Substances 0.000 title abstract 7
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 title 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 26
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 26
- 239000000428 dust Substances 0.000 claims abstract description 16
- 238000000034 method Methods 0.000 claims abstract description 7
- 239000012717 electrostatic precipitator Substances 0.000 claims description 37
- 238000011144 upstream manufacturing Methods 0.000 claims description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 87
- 229910000069 nitrogen hydride Inorganic materials 0.000 abstract description 29
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 abstract description 21
- 229910052921 ammonium sulfate Inorganic materials 0.000 abstract description 21
- 235000011130 ammonium sulphate Nutrition 0.000 abstract description 21
- 238000002347 injection Methods 0.000 abstract description 11
- 239000007924 injection Substances 0.000 abstract description 11
- 238000005260 corrosion Methods 0.000 abstract description 9
- 230000007797 corrosion Effects 0.000 abstract description 9
- 229910021529 ammonia Inorganic materials 0.000 abstract description 8
- 239000000295 fuel oil Substances 0.000 abstract description 4
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 abstract 4
- 239000007789 gas Substances 0.000 description 38
- 230000002378 acidificating effect Effects 0.000 description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 6
- 239000003546 flue gas Substances 0.000 description 6
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 230000023556 desulfurization Effects 0.000 description 5
- 239000008235 industrial water Substances 0.000 description 5
- 230000009972 noncorrosive effect Effects 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 2
- 239000002956 ash Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000004071 soot Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- GSWAOPJLTADLTN-UHFFFAOYSA-N oxidanimine Chemical compound [O-][NH3+] GSWAOPJLTADLTN-UHFFFAOYSA-N 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Electrostatic Separation (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、排ガス中のばいじん及びＳＯ３をアンモニア
を注入して電気集じん器にて捕集する場合のアンモニア
の注入によるＳＯ３の捕集方法に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention provides a method for collecting SO3 by injecting ammonia when soot and SO3 in exhaust gas is injected with ammonia and collected by an electrostatic precipitator. Regarding.
従来、油焚ボイラ排ガス中のばいじん及びＳＯ３を除去
する方法として、電気集じん器の上流側にアンモニアガ
スを注入し、ＳＯ３分を硫酸アンモニウム（硫安）（（
ＮＨ４）２ｓ０４）として未燃分あるいはアツシェ分と
ともに電気集じん器にて捕集する方法が採用されている
。この系統を第３図に示す。Conventionally, as a method for removing dust and SO3 from oil-fired boiler exhaust gas, ammonia gas was injected into the upstream side of the electrostatic precipitator, and the amount of SO3 was removed using ammonium sulfate (ammonium sulfate) ((
A method has been adopted in which NH4)2s04) is collected together with unburned or ashes by an electrostatic precipitator. This system is shown in Figure 3.
ボイラ１出口の排ガスは、必要により排煙脱硝装置２で
ＮＯｘが除去され、空気予熱器３において排熱回収が行
われた後、アンモニア注入装置７によりアンモニアガス
が注入され、電気集じん器４においてＳＯ３は酸アンモ
ニウムとして未燃分及びアツシェ分とともに除去される
。From the exhaust gas at the outlet of the boiler 1, NOx is removed by a flue gas denitrification device 2 if necessary, and exhaust heat is recovered by an air preheater 3. After that, ammonia gas is injected by an ammonia injection device 7, and then passed through an electrostatic precipitator 4. In the process, SO3 is removed as ammonium oxide along with unburned and ashes components.
除じん後の排ガスは、必要によりさらに排煙脱硫装置５
でＳｏ工が除去された後、煙突６より大気中へ放出され
る。The flue gas after dust removal is further processed by flue gas desulfurization equipment 5 if necessary.
After the SO is removed, it is released into the atmosphere from the chimney 6.
この従来の方法において、燃料中のイオウ分が高く排ガ
ス中のＳＯ３濃度が高い場合、空気予熱器３の低温部伝
熱エレメントの腐蝕を防止するため、空気予熱器３出口
の排ガス温度はあまり下げることができず、低イオウ油
燃焼の場合を比較し空気予熱器出口のガス温度は通常２
０〜４０℃程度高くなる。In this conventional method, when the sulfur content in the fuel is high and the SO3 concentration in the exhaust gas is high, the exhaust gas temperature at the outlet of the air preheater 3 is not lowered too much in order to prevent corrosion of the low temperature heat transfer element of the air preheater 3. Compared to the case of low sulfur oil combustion, the gas temperature at the outlet of the air preheater is usually 2.
The temperature increases by about 0 to 40°C.
上記従来の方法において、上記の通り電気集じん器入口
での排ガス温度が高くなると、電気集じん器にて捕集し
ようとする硫酸アンモニウム分の蒸気圧が高くなり分解
しやすくなる。硫酸アンモニウム分が分解すると、下式
のよ５に酸性硫酸アンモニウム（ＮＨ４Ｈ３Ｏ，）を生
成するが、これは腐蝕性があり電気集じん器の電極を腐
蝕させる等の障害をおこす。In the conventional method, as described above, when the temperature of the exhaust gas at the inlet of the electrostatic precipitator increases, the vapor pressure of ammonium sulfate that is to be collected by the electrostatic precipitator increases, making it easier to decompose. When the ammonium sulfate component is decomposed, acidic ammonium sulfate (NH4H3O,) is generated as shown in the following formula 5, but this is corrosive and causes problems such as corroding the electrodes of the electrostatic precipitator.
（ＮＨ４）２Ｓｏ４（固体）→ＮＨ４Ｈ３Ｏ４（液）十
ＮＨ３（ガス）↑この対策として、電気集じん器入口に
注入されるＮＨ３の濃度を高くし上記の分解反応を抑制
する運転が必要となるが、この場合には、相対的に！気
集じん器出口のＮＨ３濃度が高くなり、大気中に高濃度
のＮＨ３が放出されたり、又は排煙脱硫装置入口のアン
モニア濃度が高くなるため、排煙脱硫装置の排水中のＮ
Ｈ３濃度が高くなる等の問題があった０
本発明の目的は、上記の問題点を解決しようとするもの
である。(NH4) 2So4 (solid) → NH4H3O4 (liquid) 1NH3 (gas) ↑ As a countermeasure to this, it is necessary to increase the concentration of NH3 injected into the electrostatic precipitator inlet to suppress the above decomposition reaction. , in this case, relatively! The NH3 concentration at the outlet of the air precipitator becomes high, and a high concentration of NH3 is released into the atmosphere, or the ammonia concentration at the flue gas desulfurization equipment inlet increases, resulting in a decrease in N in the wastewater of the flue gas desulfurization equipment.
There were problems such as an increase in H3 concentration.An object of the present invention is to solve the above problems.
本発明は、電気集じん器によって排ガス中のばいじん、
及びＳＯ３を除去するに際して、電気集じん器の上流側
においてアンモニア水を排ガス中に注入し、同アンモニ
ア水中のＮＨ３の量を排ガス中の８０３に対してモル比
で２以上とし、かつ、排ガス温度が１５０℃以下好もし
くは１４０℃以下となるように同アンモニア水を注入す
ることを特徴とする。The present invention uses an electrostatic precipitator to remove soot and dust from exhaust gas.
When removing SO3, ammonia water is injected into the exhaust gas on the upstream side of the electrostatic precipitator, and the amount of NH3 in the ammonia water is set to 2 or more in molar ratio to 803 in the exhaust gas, and the exhaust gas temperature is The ammonia water is injected so that the temperature is preferably 150°C or lower or 140°C or lower.
本発明においては、
（１）電気集じん器入口の排ガス温度を１５０℃以下に
下げることによって、電気集じん器内で生成する硫酸ア
ンモニウム系化合物の蒸気圧が下るので、アンモニアの
注入量を低くでき、電気集じん器出口のＮＨ３濃度は低
く抑えられると共に、酸性硫酸アンモニウムの発生が抑
えられて、電気集じん器の電極等の腐蝕が防止される。In the present invention, (1) By lowering the exhaust gas temperature at the inlet of the electrostatic precipitator to 150°C or less, the vapor pressure of ammonium sulfate-based compounds generated in the electrostatic precipitator is lowered, so the amount of ammonia injection can be reduced. The NH3 concentration at the outlet of the electrostatic precipitator is suppressed to a low level, and the generation of acidic ammonium sulfate is suppressed, thereby preventing corrosion of the electrodes of the electrostatic precipitator.
１２７ ＮＨ３は次式＋１）のように硫酸アンモニウ
ム（硫安）を発生するが、ＮＨ３がＳＯ３に対してモル
比２以下の場合には、次式（２）の反応によって一部酸
性硫酸アンモニウムが発生する。127 NH3 generates ammonium sulfate (ammonium sulfate) as shown in the following formula +1), but when the molar ratio of NH3 to SO3 is 2 or less, acidic ammonium sulfate is partially generated by the reaction of the following formula (2).
２ＮＨ３＋ＳＯ３＋Ｈ２０→（ＮＨ，）２Ｓｏ４ ・
・・・・・・・佃ＮＨ３＋ＳＯ３＋Ｈ２０→（ＮＨ４）
２ＳＯ４・・・・・・・・・（２）本発明では、注入さ
れるＮＨ３の量を、排ガス中のＳＯ３に対しモル比で２
以上にすることによって、ＳＯ３は腐蝕性のない硫酸ア
ンモニウムとして捕集されることになる。2NH3+SO3+H20→(NH,)2So4 ・
...... Tsukuda NH3 + SO3 + H20 → (NH4)
2SO4・・・・・・(2) In the present invention, the amount of NH3 injected is set at a molar ratio of 2 to SO3 in the exhaust gas.
By doing the above, SO3 will be collected as non-corrosive ammonium sulfate.
（３）だとえＳＯ３あるいはＮＨ３のアンバランスによ
り、ＮＨ３がＳＯ３に対しモル比２以下となり一部酸性
硫酸アンモニウム（ＮＨ４Ｈ８Ｏ４）が生成する場合に
おいても、ガス温度を１５０℃以下に保持することによ
り、酸性硫酸アンモニウムは腐蝕性のない固体状として
捕集される。(3) Even if the molar ratio of NH3 to SO3 is less than 2 due to SO3 or NH3 imbalance and some acidic ammonium sulfate (NH4H8O4) is generated, by maintaining the gas temperature at 150°C or less, Acidic ammonium sulfate is collected as a non-corrosive solid.
第１図に本発明の一実施例の排ガスの７０−図を示す。 FIG. 1 shows a diagram 70 of exhaust gas according to an embodiment of the present invention.
図中符号１〜７は、第３図に示す従来の方法におけると
同一であるので説明を省略する。Reference numerals 1 to 7 in the figure are the same as those in the conventional method shown in FIG. 3, so their explanation will be omitted.
１０は、電気集じん器４の上流側の空気予熱器３と電気
集じん器４との間に設けられたアンモニア水注入装置で
あり、同アンモニア水注入装置１０には流量制御弁１６
を備えたライン１４が設けられ、同ライン１４からアン
モニア水が排ガス中に注入される。また、同アンモニア
水注入装置１０には、流量制御弁１３を備えたライン１
４に開口する工業用水の供給ライン１５が設げられてお
り、ライン１４より排ガス中に注入されるアンモニア水
中の水の量が調整されるようになっている。10 is an ammonia water injection device provided between the air preheater 3 and the electrostatic precipitator 4 on the upstream side of the electrostatic precipitator 4, and the ammonia water injection device 10 includes a flow control valve 16.
A line 14 is provided, through which aqueous ammonia is injected into the exhaust gas. The ammonia water injection device 10 also includes a line 1 equipped with a flow control valve 13.
An industrial water supply line 15 is provided which opens into the exhaust gas, and the amount of water in the ammonia water injected into the exhaust gas from the line 14 is adjusted.
本実施例で排ガス中に注入されるＮＨ３の量は、ライン
１４の流量制御弁１６によって、重油焚ボイラ１の負荷
に応じた量となるようにフントロールされる。In this embodiment, the amount of NH3 injected into the exhaust gas is controlled by the flow rate control valve 16 of the line 14 so that the amount corresponds to the load of the heavy oil-fired boiler 1.
重油中のＳ（硫黄分）は判明しており、これにより８０
３分の濃度を算出することが可能であるために、ボイラ
１に投入された燃料（重油）によるＳＯ３量が算出され
るので、この８０３量に応じて、ライン１４から排ガス
中に注入されるＮＨ３の量が、排ガス中のＳＯ３に対し
てモル比で２以上になるようにアンモニア水注入量が調
整される。The S (sulfur content) in heavy oil has been determined, and it is 80
Since it is possible to calculate the concentration for 3 minutes, the amount of SO3 due to the fuel (heavy oil) input into the boiler 1 is calculated, and according to this 803 amount, it is injected into the exhaust gas from the line 14. The amount of ammonia water injected is adjusted so that the molar ratio of the amount of NH3 to SO3 in the exhaust gas is 2 or more.
また、電気集塵器４の後流に温度コントローラ１１を設
け、この信号を制御装置１２に送り、工業用水注入装置
の流量制御弁１３を制御して、工業用水の注入量を変化
させ、電気集塵器４の入口部の排ガス温度を１５０℃以
下となるように調整する。Further, a temperature controller 11 is provided downstream of the electrostatic precipitator 4, and this signal is sent to the control device 12 to control the flow rate control valve 13 of the industrial water injection device to change the amount of industrial water injected. The exhaust gas temperature at the inlet of the dust collector 4 is adjusted to 150°C or less.
本実施例においては、上記のように、電気集じん器４の
上流において排ガス中にアンモニア水ヲ注入し、ライン
１５を経て供給される工業用水を調節することによって
同アンモニア水中の水の量を調整し、電気集じん器４人
口の排ガス温度を１５０℃以下に下げることによって、
電気集じん器４内で生成される硫酸アンモニウム系化合
物の蒸気圧を下げ、従ってＮＨ３の注入量を低くし電気
集じん器用口のＮＨ３濃度を下げることができると共Ｋ
、酸性硫酸アンモニウムの発生を抑制し、電気集じん器
の集じん板／放電極の腐蝕を防ぐことができる。また、
注入されるアンモニア水中のＮＨ３の量を排ガス中の８
０３に対してモル比で２以上とすることによって、ＳＯ
３を腐蝕性のない硫酸アンモニウムとして電気集じん器
４で捕集することができる。In this embodiment, as described above, ammonia water is injected into the exhaust gas upstream of the electrostatic precipitator 4, and the amount of water in the ammonia water is controlled by adjusting the industrial water supplied via the line 15. By adjusting and lowering the exhaust gas temperature of the electrostatic precipitator 4 to below 150℃,
It is possible to lower the vapor pressure of ammonium sulfate-based compounds generated in the electrostatic precipitator 4, thereby lowering the injection amount of NH3 and lowering the NH3 concentration at the electrostatic precipitator inlet.
It is possible to suppress the generation of acidic ammonium sulfate and prevent corrosion of the dust collecting plate/discharge electrode of an electrostatic precipitator. Also,
The amount of NH3 in the injected ammonia water is calculated from 8 in the exhaust gas.
By setting the molar ratio to 03 to 2 or more, SO
3 can be collected by an electrostatic precipitator 4 as non-corrosive ammonium sulfate.
また、ＳＯ３又はＮＨ３のアンバランスによって、ＮＨ
３が８０３に対してモル比２以下となって、一部酸性硫
酸アンモニウムが生成しても、ガス温度を１５０℃以下
にすることによって、酸性硫酸アンモニウムを腐蝕性の
ない固体状として電気集じん器４によって捕集すること
ができる。Also, due to imbalance of SO3 or NH3, NH
Even if the molar ratio of 3 to 803 is 2 or less and some acidic ammonium sulfate is generated, by lowering the gas temperature to 150°C or less, the acidic ammonium sulfate is converted into a non-corrosive solid state and the electrostatic precipitator 4 can be collected by
本実施例の効果を実証するために第２図に示すパイロッ
トプラントを設け、実験を行なった。In order to demonstrate the effects of this example, a pilot plant shown in FIG. 2 was set up and an experiment was conducted.
即ち１重油焚ボイラ（８分約３チ）の空気予熱器３の出
口より、第２図に示すように排ガスの１部１０．ＯＯＱ
Ｎｍ’／Ｈを取出すバイパスを設け、同バイパスに第１
図に示すアンモニア水注入設備ｌＯ′及びその下流に電
気集じん器４′を設けると共に、このバイパスを電気集
じん器４′の上流で排ガス通路に接続したノセイロット
プラントを設置した。アンモニア水注入部の排ガス性状
は、次のとおりであった。That is, from the outlet of the air preheater 3 of the single heavy oil fired boiler (approximately 3 inches for 8 minutes), a portion of the exhaust gas 10. OOQ
A bypass is provided to take out Nm'/H, and a first
A nocelot plant was installed in which an ammonia water injection facility 10' shown in the figure and an electrostatic precipitator 4' were installed downstream thereof, and this bypass was connected to the exhaust gas passage upstream of the electrostatic precipitator 4'. The exhaust gas properties of the ammonia water injection section were as follows.
ガス量： １０．００ ＯＮｍ３／’Ｈｌ ガス温度
： １６０〜１５０℃。Gas amount: 10.00 ONm3/'Hl Gas temperature: 160-150°C.
０２濃度２８〜４％、 ＮＯｘ濃度：２００ｐｙ
ｎ＊５ＯＸｅｋ度＝１５００〜１３００ｐｐｍ、ＳＯ３
濃Ｉｆ ： ４５〜４０ ｐｐｍ。02 concentration 28-4%, NOx concentration: 200py
n*5OXek degree=1500~1300ppm, SO3
Concentration If: 45-40 ppm.
ばいじん濃度： ２００〜２５０Ｉｎ９／Ｎｍ 。Dust concentration: 200-250In9/Nm.
〔比較例−１〕
アンモニア水を使用せず、ガス状アンモニアを空気で希
釈してパイロットプラント電気集じん器４′上流におい
て上記性状の排ガスに注入し、同電気集じん器４′入口
のＮＨ３濃度を１００〜１１０ｐｐｍとした。[Comparative Example-1] Without using ammonia water, gaseous ammonia was diluted with air and injected into the exhaust gas having the above properties upstream of the pilot plant electrostatic precipitator 4', and the NH3 at the inlet of the electrostatic precipitator 4' was The concentration was 100-110 ppm.
この状態で１ケ月間運用後、装置を停止し電気集じん器
４′内部を開放点検した結果、集じん板／放電極ともに
腐蝕が見られ、一部ダストの固着も見られた。本期間中
の電気集じん器４′出口のＮＨ３濃度は１０ ｐｐｍ８
度であった。After operating in this state for one month, the equipment was stopped and the inside of the electrostatic precipitator 4' was opened and inspected. As a result, corrosion was observed on both the dust collecting plate and the discharge electrode, and some dust was observed to adhere. During this period, the NH3 concentration at the electrostatic precipitator 4' outlet was 10 ppm8
It was degree.
〔比較例−２〕
上記と同様の条件で、 ＮＨ３濃度を１００〜１１０ｐ
ｐｍから２００〜２５０ｐｐｍに上昇させ１ケ月間運用
後、装置を停止しＥＰ内部を開放点検の結果、集じん板
／放電極の腐蝕やダストの固着は見られなかった。[Comparative Example-2] Under the same conditions as above, the NH3 concentration was set to 100 to 110p.
After increasing the pm from 200 to 250 ppm and operating for one month, the equipment was stopped and the inside of the EP was opened and inspected. As a result, no corrosion of the dust collector plate/discharge electrode or adhesion of dust was observed.
しかし１本期間中の電気集じん器４′出口のＮＨ３濃度
は１１０〜１６０ ｐｐｍで１＞ツた。However, the NH3 concentration at the outlet of the electrostatic precipitator 4' during one period was 110 to 160 ppm.
下記の性状の排ガスにガス状アンモニアに代えてアンモ
ニア水を使用し、電気集じん器４人ロ排ガス性状を以下
のとおり調整した。Aqueous ammonia was used instead of gaseous ammonia for the exhaust gas having the following properties, and the properties of the exhaust gas were adjusted as follows using an electrostatic precipitator for four people.
ガス量： １００００ Ｎｍ３Ａ、温度：１４０℃。Gas amount: 10,000 Nm3A, temperature: 140°C.
０２濃度：４〜８％、 ＮｏＸ濃度： ２００ ｐ
ｐｍ。02 concentration: 4-8%, NoX concentration: 200p
p.m.
ＳＯｘ濃度：１５００〜１３００ｐｐｍ、 Ｓｏ３濃度
： ４０〜４５ ｐｐｍ。SOx concentration: 1500-1300 ppm, So3 concentration: 40-45 ppm.
ＮＨ３濃度： １００〜１１０ｐｐｍ、ばいじん濃度：
２００〜２５（７％、：上記の条件で、１ケ月間運用
後、装置を停止しＥＰ内部を開放点検の結果、集じん板
／放電極の腐蝕やダストの固着は見られなかった。本期
間中の電気集じん器４′出口のＮＨ３濃度は１０ ｐｐ
ｍ程度であった。NH3 concentration: 100-110ppm, dust concentration:
200 to 25 (7%): After operating for one month under the above conditions, the equipment was stopped and the inside of the EP was opened and inspected, and no corrosion or dust adhesion was found on the dust collector plate/discharge electrode.Book During the period, the NH3 concentration at the electrostatic precipitator 4' outlet was 10 pp.
It was about m.
本発明は次の効果を奏することができる。 The present invention can have the following effects.
（１） アンモニア水を注入して電気集塵器入口の排
ガス温度を１５０℃以下に下げることにより、排ガス中
へのＮＨ３の注入量を低くすることができ、出口のＮＨ
３濃度を低くすることができる。また、ＳＯ３あるいは
ＮＨ３のアンバランスが起こっても、温度が１５０℃以
下となっているために１酸性硫酸アンモニウム（ＮＨ４
Ｈ３Ｏ４）を腐蝕性のない固体状として捕集することが
でき、集塵器内部の電極等の腐蝕を防止することができ
る。(1) By injecting ammonia water to lower the exhaust gas temperature at the electrostatic precipitator inlet to 150°C or less, the amount of NH3 injected into the exhaust gas can be lowered, and the NH3 at the outlet can be lowered.
3. The concentration can be lowered. Furthermore, even if SO3 or NH3 imbalance occurs, monoacid ammonium sulfate (NH4
H3O4) can be collected in a non-corrosive solid state, and corrosion of the electrodes inside the dust collector can be prevented.
（２）注入されるＮＨ３を排ガス中の８０３に対し、モ
ル比で２以上とすることにより、ＳＯ３を硫酸アンモニ
ウム（（ＮＨ４）２Ｓｏ４） の固体状として捕集す
ることができる。(2) By setting the molar ratio of injected NH3 to 803 in the exhaust gas to be 2 or more, SO3 can be collected in the form of solid ammonium sulfate ((NH4)2So4).
第１図は本発明の一実施例のフロー図、第２図は同実施
例の実験に用いられたパイロットプラントのフロー図、
第３図は従来のボイラの脱硫硝方法を示すフロー図であ
る。
１・・・ボイラ、２．５・・・排煙脱硫装置。
３・・・空気予熱器、 ４・・・電気集じん器。
１０・・・アンモニア水注入装置。
１１・・・温度コントローラ、 １３．１６・・・流
量制御弁。
１４・・・アンモニア水ライン、１５・・・工業水ライ
ン。
代理人 弁理士 坂 間 暁
外２名Figure 1 is a flow diagram of an embodiment of the present invention, Figure 2 is a flow diagram of a pilot plant used in experiments of the same embodiment,
FIG. 3 is a flow diagram showing a conventional boiler desulfurization method. 1... Boiler, 2.5... Flue gas desulfurization equipment. 3...Air preheater, 4...Electrostatic precipitator. 10...Ammonia water injection device. 11...Temperature controller, 13.16...Flow rate control valve. 14... Ammonia water line, 15... Industrial water line. Agent: Patent attorney Akigai Sakama (2 people)
Claims (1)
３を除去するに際して、電気集じん器の上流側において
、アンモニア水を排ガス中に注入し、同アンモニア水中
のＮＨ＿３の量を排ガス中のＳＯ＿３に対してモル比で
２以上とし、かつ、排ガス温度が１５０℃以下となるよ
うに同アンモニア水を注入することを特徴とする排ガス
のＳＯ＿３捕集方法。Dust and SO_ in exhaust gas by electrostatic precipitator
When removing 3, ammonia water is injected into the exhaust gas on the upstream side of the electrostatic precipitator, and the molar ratio of NH_3 in the ammonia water to SO_3 in the exhaust gas is 2 or more, and the exhaust gas temperature is A method for collecting SO_3 from exhaust gas, characterized by injecting the same ammonia water so that the temperature is 150°C or less.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1086845A JPH02265618A (en) | 1989-04-07 | 1989-04-07 | Capture of sulfur trioxide in waste gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1086845A JPH02265618A (en) | 1989-04-07 | 1989-04-07 | Capture of sulfur trioxide in waste gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH02265618A true JPH02265618A (en) | 1990-10-30 |
Family
ID=13898148
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1086845A Pending JPH02265618A (en) | 1989-04-07 | 1989-04-07 | Capture of sulfur trioxide in waste gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH02265618A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010234322A (en) * | 2009-03-31 | 2010-10-21 | Chugoku Electric Power Co Inc:The | Exhaust gas purification method and exhaust gas purification apparatus |
-
1989
- 1989-04-07 JP JP1086845A patent/JPH02265618A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010234322A (en) * | 2009-03-31 | 2010-10-21 | Chugoku Electric Power Co Inc:The | Exhaust gas purification method and exhaust gas purification apparatus |
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