JPS6153106B2 - - Google Patents
Info
- Publication number
- JPS6153106B2 JPS6153106B2 JP12518380A JP12518380A JPS6153106B2 JP S6153106 B2 JPS6153106 B2 JP S6153106B2 JP 12518380 A JP12518380 A JP 12518380A JP 12518380 A JP12518380 A JP 12518380A JP S6153106 B2 JPS6153106 B2 JP S6153106B2
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- electrostatic precipitator
- gas treatment
- dust collection
- coal
- 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
Links
- 239000012717 electrostatic precipitator Substances 0.000 claims description 21
- 238000000034 method Methods 0.000 claims description 8
- 238000006477 desulfuration reaction Methods 0.000 claims description 6
- 230000023556 desulfurization Effects 0.000 claims description 6
- 238000001179 sorption measurement Methods 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 239000000428 dust Substances 0.000 description 16
- 229910052717 sulfur Inorganic materials 0.000 description 9
- 239000011593 sulfur Substances 0.000 description 9
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 8
- 239000003245 coal Substances 0.000 description 6
- 238000002347 injection Methods 0.000 description 6
- 239000007924 injection Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 239000010881 fly ash Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 230000005611 electricity Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
- B03C3/01—Pretreatment of the gases prior to electrostatic precipitation
- B03C3/013—Conditioning by chemical additives, e.g. with SO3
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Electrostatic Separation (AREA)
Description
【発明の詳細な説明】
本発明は石炭焚きボイラー等用電気集塵装置の
集塵率を向上させるための排ガス処理方法に関す
るものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an exhaust gas treatment method for improving the dust collection efficiency of an electrostatic precipitator for a coal-fired boiler or the like.
石炭焚きボイラー等用電気集塵装置は石炭中の
硫黄分により集塵率が大きく変化し、特に硫黄分
１％以下の低硫黄炭を燃焼した場合に発生するフ
ライアツシユは電気抵抗が高くて電気集塵装置の
集塵率を悪くする。このため従来、低硫黄炭を使
用する場合は電気集塵装置を非常に大きく設計
し、また、さらに電気抵抗の高いフライアツシユ
が生ずる石炭を使用する場合は電気集塵装置の上
流ダクトNH3又はSO3を注入して排ガス処理を行
なつていた。 The dust collection rate of electrostatic precipitators for coal-fired boilers varies greatly depending on the sulfur content in the coal. In particular, the fly ash generated when low-sulfur coal with a sulfur content of 1% or less has a high electrical resistance and cannot be used as an electrostatic precipitator. Decrease the dust collection rate of the dust device. For this reason, conventionally, when using low-sulfur coal, the electrostatic precipitator is designed to be very large, and when using coal that produces fly ash with high electrical resistance, the upstream duct of the electrostatic precipitator is designed to be 3 was injected to treat exhaust gas.
しかしながら、従来の排ガス処理用原材料とし
てNH3やSO3発生用のH2SO4、液体SO3、液体
SO2、固体硫黄等を購入しており、価格が高く、
また購入後の貯蔵問題がある他、排ガス処理装置
が簡単にできなかつた。高価な液体SO3を使用す
る排ガス処理にあつてはさらに高価となり、また
装置が複雑となり、危検性があるなどの問題もあ
つた。 However, conventional raw materials for exhaust gas treatment include H 2 SO 4 for NH 3 and SO 3 generation, liquid SO 3 , and liquid
We purchase SO 2 , solid sulfur, etc., and the prices are high.
In addition to the problem of storage after purchase, it was not easy to install exhaust gas treatment equipment. Exhaust gas treatment using expensive liquid SO 3 is even more expensive, and the equipment is complicated, leading to problems such as danger.
ところで、排ガス処理方法には、ボイラーから
の排ガス中のSO3濃度と集塵率との関係を例示す
る第１図で分るようにSO3濃度を10p.p.m程度と
すれば集塵率を大巾に向上させうると共に、SO3
濃度の所定の集塵率を得る電気集塵装置の大きさ
との関係を例示する第２図で分るように該集塵率
を得るためにはSO3濃度を10p.p.m程度とすれば
電気集塵装置の規膜を高硫黄炭を燃焼するボイラ
ー用のもの程度にとどめることができるという２
つの利点がある。 By the way, in the exhaust gas treatment method, as shown in Figure 1, which shows the relationship between the SO 3 concentration in the exhaust gas from the boiler and the dust collection rate, if the SO 3 concentration is about 10 p.pm, the dust collection rate can be increased. It can be greatly improved and SO 3
As can be seen in Figure 2, which illustrates the relationship between the size of the electrostatic precipitator and the size of the electrostatic precipitator to obtain a predetermined dust collection rate, in order to obtain the dust collection rate, if the SO 3 concentration is about 10 p.pm, the electricity It is said that the diaphragm of the dust collector can be kept to the same level as that used in boilers that burn high sulfur coal.
There are two advantages.
本発明は前記従来の問題点を解決して排ガス処
理方法の前記利点を活かすために創案されたもの
で、電気集塵装置の下流ダクトから脱硫装置及び
吸着SO2ガス脱離器により濃縮SO2ガスが得られ
ることに着目しその一部を排ガス処理用として
SO3に転換使用することにより、従来のような排
ガス処理用原材料の購入貯蔵等の問題をなくし、
また従来に比し排ガス処理装置を簡単にし、さら
に排ガス処理を行なわずにフライアツシユに対処
する場合のものに比し電気集塵装置を小型化する
ことができ、またSO3注入量の抑制を容易化で
き、さらにその制御性と相俟つて安定した集塵率
を得ることができる。排ガス処理方法を提供する
ことを目的とするものである。 The present invention was devised to solve the above-mentioned conventional problems and take advantage of the above-mentioned advantages of the exhaust gas treatment method . Focusing on the fact that gas can be obtained, some of it is used for exhaust gas treatment.
By converting and using SO 3 , we eliminate the conventional problems of purchasing and storing raw materials for exhaust gas treatment.
In addition, the exhaust gas treatment equipment is simpler than conventional equipment, and the electrostatic precipitator can be made smaller compared to those that deal with fly ash without exhaust gas treatment, and the amount of SO 3 injection can be easily controlled. Furthermore, in combination with its controllability, a stable dust collection rate can be obtained. The object of the present invention is to provide an exhaust gas treatment method.
以下、本発明を実施する装置を第３図により説
明すると、石炭焚きのボイラー１から煙突２に到
るダクト３にはNOx除去用脱硝装置４、排熱回収
用空気予熱器５、電気集塵装置６、誘引通風機
７、乾式脱硫装置８、昇圧通風機９及びバグフイ
ルタ１０が順次配され、脱硫装置８には吸着SO2
ガス脱離器１１を介し硫黄回収装置１２が接続さ
れると共にこれら１１，１２間にてブロワ１３を
介して、SO3転化器１４が接続され、このSO3転
化器１４は前記電気集塵装置６の入口に近くダク
ト３に設けたSO3注入用ノズル（図示せず）に接
続されている。 Hereinafter, an apparatus for carrying out the present invention will be explained with reference to FIG. 3. A duct 3 leading from a coal-fired boiler 1 to a chimney 2 includes a denitrification device 4 for removing NOx , an air preheater 5 for exhaust heat recovery, and an electric collector. A dust device 6, an induced draft fan 7, a dry desulfurization device 8, a booster draft fan 9, and a bag filter 10 are arranged in sequence, and the desulfurization device 8 absorbs SO 2
A sulfur recovery device 12 is connected via a gas desorber 11, and an SO 3 converter 14 is connected between these 11 and 12 via a blower 13, and this SO 3 converter 14 is connected to the electrostatic precipitator. It is connected to an SO 3 injection nozzle (not shown) provided in the duct 3 near the inlet of the duct 6.
以上の装置構成において、ボイラー１で発生し
た排ガスは、脱硝装置４、空気予熱器５を通り電
気集塵装置６に入る。このときの排ガス中のSO2
濃度は石炭中の硫黄分が１％の場合910p.p.m位
であり、SO3は4p.p.mである。電気集塵装置６、
誘引通風機７を経た排ガスは脱硫装置８でSO2が
95％程度除去され、バグフイルタ１０で除塵され
た後煙突２より大気中に放出される。脱硫装置８
で除去されたSO2は吸着SO2ガス脱離器１１によ
り脱離され10〜20重量％の濃度となり硫黄回収装
置１２により単体硫黄として回収される。 In the above device configuration, the exhaust gas generated in the boiler 1 passes through the denitrification device 4 and the air preheater 5 and enters the electrostatic precipitator 6. SO 2 in the exhaust gas at this time
When the sulfur content in coal is 1%, the concentration is about 910 p.pm, and SO 3 is 4 p.pm. electrostatic precipitator 6,
The exhaust gas that has passed through the induced draft fan 7 is converted into SO 2 by the desulfurization device 8.
Approximately 95% of the dust is removed, and after being removed by a bag filter 10, it is released into the atmosphere from a chimney 2. Desulfurization equipment 8
The SO 2 removed is desorbed by the adsorption SO 2 gas desorber 11 and has a concentration of 10 to 20% by weight, and is recovered as elemental sulfur by the sulfur recovery device 12.
本発明は上記フローにおいて吸着SO2ガス脱離
器１１から出た濃度SO2ガスの一部をブロワ１２
による引きでSO3転化器１４に送りそこでSO3に
転化して電気集塵装置６の上流ダクト３に該装置
６の入口ガス中のSO3濃度が10p.p.m程度となる
ようにノズルにより注入するものである。 In the present invention, in the above flow, a part of the concentrated SO 2 gas discharged from the adsorbed SO 2 gas desorber 11 is transferred to the blower 12.
The SO 3 is sent to the SO 3 converter 14, where it is converted to SO 3 , and injected into the upstream duct 3 of the electrostatic precipitator 6 through a nozzle so that the SO 3 concentration in the inlet gas of the device 6 is about 10 p.pm. It is something to do.
SO3注入量の制御方法としては、電気集塵装置
６の出口ガス中のSO2を検出してその量に応じて
SO3注入量を制御するもの、電気集塵装置６の電
圧及び電流を検出しこれらがある値より低下した
場合にその低下度によりSO3注入量を制御するも
の、また電気集塵装置の出口の煤塵量を検出して
その増減によりSO3注入量を増減するもの等、
種々の方法を採ればよい。 The method of controlling the amount of SO 3 injection is to detect SO 2 in the outlet gas of the electrostatic precipitator 6 and adjust the amount accordingly.
A device that controls the amount of SO 3 injection, a device that detects the voltage and current of the electrostatic precipitator 6 and controls the amount of SO 3 injection depending on the degree of decrease when these drop below a certain value, and an outlet of the electrostatic precipitator 6. such as those that detect the amount of soot and dust and increase or decrease the amount of SO 3 injection depending on the increase or decrease in the amount.
Various methods may be used.
本発明は以上の通り電気集塵装置の上流ダクト
に注入するSO3を、該装置の下流ダクトから脱硫
装置及び吸着SO2ガス脱離器により得た濃縮SO2
ガスの一部を転化してつくりだす簡単な構成であ
るため、排ガス処理装置が簡単となることを相俟
つて、SO3注入量の制御が容易となり、排ガス中
のSO3濃度のコントロールで集塵率を大巾に向上
安定させることができると共に、電気集塵装置自
体を小さく安価に設計できる。また、SO3発生用
原材料を別途に購入貯蔵する必要がなくなりそれ
だけさらに安価で済む。さらに、前記の如く排ガ
ス装置が簡単となるためその取扱いも容易化で
き、またメンテナンスを軽減できる等の効果を有
する。 As described above, the present invention converts SO 3 to be injected into the upstream duct of an electrostatic precipitator into concentrated SO 2 obtained from the downstream duct of the device by a desulfurization device and an adsorption SO 2 gas desorber.
Because it has a simple configuration that generates gas by converting a part of it, the exhaust gas treatment equipment is simple, and the amount of SO 3 injected can be easily controlled, making it possible to collect dust by controlling the SO 3 concentration in the exhaust gas. The rate can be greatly improved and stabilized, and the electrostatic precipitator itself can be designed to be small and inexpensive. In addition, there is no need to separately purchase and store raw materials for SO 3 generation, resulting in even lower costs. Furthermore, as mentioned above, since the exhaust gas device is simple, it can be handled easily and maintenance can be reduced.
第１図は排ガス中のSO3濃度と集塵率との関係
を例示する線図、第２図は排ガス中のSO3濃度と
所定集塵率を得る電気集塵装置の大きさとの関係
を例示する線図、第３図は本発明の一実施例の装
置の概要図である。
１……ボイラー、３……ダクト、６……電気集
塵装置、８……脱硫装置、１１……吸着SO2ガス
脱離器、１３……ブロワ、１４……SO3転化器。
Figure 1 is a diagram illustrating the relationship between the SO 3 concentration in exhaust gas and the dust collection rate, and Figure 2 is a diagram illustrating the relationship between the SO 3 concentration in exhaust gas and the size of the electrostatic precipitator that obtains a predetermined dust collection rate. The illustrative diagram, FIG. 3, is a schematic diagram of an apparatus according to one embodiment of the present invention. 1...Boiler, 3...Duct, 6...Electrostatic precipitator, 8...Desulfurizer, 11...Adsorption SO2 gas desorber, 13...Blower, 14... SO3 converter.
Claims (1)
硫装置に順次通過させて処理する方法において、
吸着SO2ガス脱離器で脱離された濃縮SO2ガスの
一部をSO3転化器でSO3に転化して前記電気集塵
装置の上流側ダクトに注入することを特徴とする
排ガス処理方法。1. In a method of processing boiler exhaust gas by sequentially passing it through a denitrification device, an electrostatic precipitator, and a desulfurization device,
An exhaust gas treatment characterized in that a part of the concentrated SO 2 gas desorbed by the adsorption SO 2 gas desorber is converted into SO 3 by an SO 3 converter and injected into the upstream duct of the electrostatic precipitator. Method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12518380A JPS5750560A (en) | 1980-09-09 | 1980-09-09 | Method for refining of waste gas for electrostatic dust precipitator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12518380A JPS5750560A (en) | 1980-09-09 | 1980-09-09 | Method for refining of waste gas for electrostatic dust precipitator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5750560A JPS5750560A (en) | 1982-03-25 |
| JPS6153106B2 true JPS6153106B2 (en) | 1986-11-15 |
Family
ID=14903950
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP12518380A Granted JPS5750560A (en) | 1980-09-09 | 1980-09-09 | Method for refining of waste gas for electrostatic dust precipitator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5750560A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102607031A (en) * | 2012-03-30 | 2012-07-25 | 许名香 | Garbage disposal method and mechanical upright kiln device without chimneys for garbage disposal |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59122407A (en) * | 1982-12-29 | 1984-07-14 | Katayama Chem Works Co Ltd | Prevention of slime obstacle of alkali paper making system |
| US5024681A (en) * | 1989-12-15 | 1991-06-18 | Electric Power Research Institute | Compact hybrid particulate collector |
| JPH05272499A (en) * | 1992-03-27 | 1993-10-19 | Nittetsu Mining Co Ltd | Powder pump |
| JP3747504B2 (en) * | 1996-02-23 | 2006-02-22 | 栗田工業株式会社 | Copper pitting corrosion prevention method |
| JP2007326079A (en) * | 2006-06-09 | 2007-12-20 | Mhi Environment Engineering Co Ltd | Flue gas treatment system and method of coal burning boiler |
| US8398744B2 (en) * | 2010-09-21 | 2013-03-19 | General Electric Company | Method and apparatus for air pollution control |
-
1980
- 1980-09-09 JP JP12518380A patent/JPS5750560A/en active Granted
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102607031A (en) * | 2012-03-30 | 2012-07-25 | 许名香 | Garbage disposal method and mechanical upright kiln device without chimneys for garbage disposal |
| CN102607031B (en) * | 2012-03-30 | 2015-08-19 | 许名香 | A kind of waste disposal method and the chimney-free boiler-turbine CCS device for garbage disposal |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5750560A (en) | 1982-03-25 |
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