JPS6345852B2 - - Google Patents
Info
- Publication number
- JPS6345852B2 JPS6345852B2 JP58057278A JP5727883A JPS6345852B2 JP S6345852 B2 JPS6345852 B2 JP S6345852B2 JP 58057278 A JP58057278 A JP 58057278A JP 5727883 A JP5727883 A JP 5727883A JP S6345852 B2 JPS6345852 B2 JP S6345852B2
- Authority
- JP
- Japan
- Prior art keywords
- dust
- cao
- exhaust gas
- caco
- sox
- 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
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Treating Waste Gases (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Chimneys And Flues (AREA)
Description
【発明の詳細な説明】
本発明は、産業廃棄物焼却炉排ガス、都市ごみ
焼却炉排ガスなど（以下、単に廃棄物焼却炉排ガ
スという）のようにHCl、SOxおよびダストを含
む排ガスを、石灰石を用いて効率よくかつ低コス
トで処理する方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention aims to convert waste gas containing HCl, SOx, and dust, such as industrial waste incinerator exhaust gas and municipal waste incinerator exhaust gas (hereinafter simply referred to as waste incinerator exhaust gas), to limestone. The present invention relates to a method for processing efficiently and at low cost.
一般に、廃棄物焼却炉排ガス、たとえば都市ご
み焼却炉排ガスにはHClが200〜1000ppm、SOx
が10〜100ppm含まれており、このHCl、SOxを
CaCO3を用いて化学反応させCaCO2、CaSO4と
して分離・除去する乾式法は従来から良く知られ
ている。この乾式法は、アルカリ水溶液に有害ガ
スを吸収、溶解させて排水として除去する湿式法
に比べて、その排水を処理しなければならないな
どの問題がなく簡易な方法であるので安価となる
という利点を有しているが、CaCO3の利用率が
それ程高くなく、また熱ロスが多いほどの問題点
があつた。 Generally, waste incinerator exhaust gas, such as municipal waste incinerator exhaust gas, contains 200 to 1000 ppm of HCl and SOx.
Contains 10 to 100 ppm, and this HCl, SOx
The dry method of chemically reacting CaCO 3 and separating and removing it as CaCO 2 and CaSO 4 has been well known. Compared to the wet method, which absorbs and dissolves harmful gases in an alkaline aqueous solution and removes them as wastewater, this dry method has the advantage that it is a simple method that does not require treatment of the wastewater and is therefore inexpensive. However, there were problems in that the utilization rate of CaCO 3 was not very high and there was a lot of heat loss.
本発明は上記の問題点を解決するためになされ
たもので、廃棄物焼却流動床炉に石灰石
（CaCO3）を投入して排ガス中のHCl、SOxを除
去する方法において、流動床炉内で活性化された
CaO、珪砂などの流動媒体、反応生成物、不燃
物、ダストの混合物を炉底から抜き出し、反応生
成物、不燃物、ダストを分離した後、CaOおよび
流動媒体を２枚の支持体間を低速度で落下させる
移動層式有害ガス・ダスト除去装置に投入して流
動床炉からの排ガスをこの移動層内に通過させ
て、CaOと排ガス中の含有HCl、SOxとを反応さ
せると同時に排ガス中のダストを捕集した後、反
応生成物およびダストとCaCO3、CaOおよび流
動媒体とに分離し、CaCO3、CaOおよび流動媒
体を再び流動床炉に供給して発生HCl、SOxの除
去に再利用することにより、低コストでHCl、
SOx、ダストを同時に除去することができる廃棄
物焼却炉排ガス中の有害成分・ダスト除去方法を
提供せんとするものである。 The present invention was made to solve the above problems, and is a method for removing HCl and SOx from exhaust gas by introducing limestone (CaCO 3 ) into a waste incineration fluidized bed furnace. activated
A mixture of CaO, a fluid medium such as silica sand, reaction products, noncombustibles, and dust is extracted from the furnace bottom, and after separating the reaction products, noncombustibles, and dust, CaO and the fluid medium are passed between two supports. The exhaust gas from the fluidized bed furnace is fed into a moving bed type harmful gas/dust removal device that drops at a high speed, and the exhaust gas from the fluidized bed furnace is passed through this moving bed to react with CaO and HCl and SOx contained in the exhaust gas. After collecting the dust of By using HCl at low cost,
The purpose of this invention is to provide a method for removing harmful components and dust from waste incinerator exhaust gas that can simultaneously remove SOx and dust.
以下、本発明の構成を図面に基づいて説明す
る。１は流動床炉で、珪砂などの流動媒体（以
下、砂という）が用いられる。流動床炉１に脱
塩・脱硫剤として一定粒径のCaCO3を投入する
と、大部分はCaOまで熱解離して活性化し、発生
HCl、SOxガスと反応し脱塩、脱硫が行なわれ
る。この反応は、CaO粒子の表面で起こり、
CaCl2や、CaSO4のような反応生成物になるが、
砂などの撹拌作用により、反応生成物ははがされ
て殆ど粉体の状態で排ガスに同伴されて流動床炉
１の上部から排出される。流動床炉１内ではつぎ
の反応が行なわれる。 Hereinafter, the configuration of the present invention will be explained based on the drawings. 1 is a fluidized bed furnace in which a fluidized medium such as silica sand (hereinafter referred to as sand) is used. When CaCO 3 of a certain particle size is introduced into the fluidized bed furnace 1 as a desalination/desulfurization agent, most of it is thermally dissociated to CaO, activated, and generated.
Reacts with HCl and SOx gas to perform desalination and desulfurization. This reaction occurs on the surface of CaO particles,
Reaction products such as CaCl 2 and CaSO 4 are produced,
Due to the stirring action of sand or the like, the reaction product is peeled off and is discharged from the upper part of the fluidized bed furnace 1 in a mostly powdered state along with the exhaust gas. The following reaction takes place in the fluidized bed furnace 1.
CaCO3→CaO＋CO2
CaO＋2HCl→CaCl2＋H2O
CaCO3＋2HCl→CaCl2＋H2O＋CO2
CaO＋SO2→CaSO3
CaSO3＋１／202→CaSO4
一方、活性化されたCaO（１部反応したCaCO2
を含む）と砂との混合物は流動床炉１の炉底から
抜き出され、３段形振動ふるいなどの分離装置２
で不燃物、ダスト、反応生成物（CaCl2、
CaSO4）を分離除去し、CaOおよび砂は移動層式
有害ガス・ダスト除去装置３へ搬送される。４は
流動媒体排出装置、５は中間ホツパ、６は余剰
CaO・砂抜出管である。CaCO 3 →CaO+CO 2 CaO+2HCl→CaCl 2 +H 2 O CaCO 3 +2HCl→CaCl 2 +H 2 O+CO 2 CaO+SO 2 →CaSO 3 CaSO 3 +1/20 2 →CaSO 4 On the other hand, activated CaO (partially reacted CaCO 2
) and sand is extracted from the bottom of the fluidized bed furnace 1 and passed through a separation device 2 such as a three-stage vibrating screen.
Incombustibles, dust, reaction products (CaCl 2 ,
CaSO 4 ) is separated and removed, and CaO and sand are transported to a moving bed type harmful gas/dust removal device 3. 4 is a fluidized medium discharge device, 5 is an intermediate hopper, and 6 is a surplus
This is a CaO/sand extraction pipe.
移動層式有害ガス・ダスト除去装置３内には、
ルーバ、孔明板、金網などからなる２枚の支持体
７が対設されており、この支持体７，７間にCaO
および砂を充填し低速度で落下する移動層８とな
るように構成されている。搬送されてきたCaOと
砂との混合物は、支持体７，７間を自重落下しつ
つ排ガスと接触し、排ガス中に含まれるHCl、
SOxガスを反応吸収すると同時に、排ガス中のダ
ストもCaOと砂との混合物の層で捕集される。な
お１０は廃熱ボイラ、ガス冷却塔、熱交換器など
の排ガス冷却装置である。移動層式有害ガス・ダ
スト除去装置３内での反応はつぎの通りである。 Inside the moving bed type harmful gas/dust removal device 3,
Two supports 7 made of louvers, perforated plates, wire mesh, etc. are placed opposite each other, and between these supports 7, CaO
The moving layer 8 is filled with sand and falls at a low speed. The conveyed mixture of CaO and sand falls between the supports 7 and 7 under its own weight and comes into contact with the exhaust gas, and the HCl contained in the exhaust gas,
At the same time as SOx gas is reacted and absorbed, dust in the exhaust gas is also collected in a layer of CaO and sand mixture. Note that 10 is an exhaust gas cooling device such as a waste heat boiler, a gas cooling tower, and a heat exchanger. The reaction within the moving bed type harmful gas/dust removal device 3 is as follows.
CaO＋2HCl→CaCl2＋H2O
CaO＋SO3→CaSO3
CaSO3＋１／202→CaSO4
CaO＋CO2→CaCO3
移動層式有害ガス・ダスト除去装置３から排出
される混合物には、ダスト、反応生成物
（CaCl2、CaSO4）が含まれているので、これを
振動ふるいなどの分離装置１１により除去し、
CaCO3、CaOおよび砂の混合物を流動床炉１に
投入し再利用する。１２は送風機、１３はサイク
ロン、１４は空気分散板、１５は風箱である。CaO+2HCl→CaCl 2 +H 2 O CaO+SO 3 →CaSO 3 CaSO 3 +1/20 2 →CaSO 4 CaO+CO 2 →CaCO 3 The mixture discharged from the moving bed harmful gas/dust removal device 3 includes dust, reaction products ( CaCl 2 , CaSO 4 ) is included, so this is removed using a separator 11 such as a vibrating sieve.
A mixture of CaCO 3 , CaO and sand is put into the fluidized bed furnace 1 and reused. 12 is a blower, 13 is a cyclone, 14 is an air distribution plate, and 15 is a wind box.
CaOと砂との混合物は炉底から抜き出された
後、移動層式有害ガス・ダスト除去装置に至るま
での間に放熱により冷却されるが、移動層式有害
ガス・ダスト除去装置３において、排ガスの顕熱
が与えられ再度加熱されるので、熱ロスを小さく
するという利点がある。なお循環して使用する流
動媒体は、Ca系と砂との混合物に限ることなく、
Ca系単独でも可能である。 After the mixture of CaO and sand is extracted from the furnace bottom, it is cooled by heat radiation before reaching the moving bed type harmful gas and dust removal device 3. Since the sensible heat of the exhaust gas is given and heated again, it has the advantage of reducing heat loss. The fluid medium to be circulated and used is not limited to a mixture of Ca-based and sand.
It is also possible to use Ca alone.
以上説明したように、本発明の方法は廃棄物焼
却流動床炉に脱塩・脱硫剤としてCaCO3を投入
し、炉内で活性化されたCaOと砂との混合物を移
動層式有害ガス・ダクト除去装置の反応剤兼ろ過
材として用い、排ガスに含まれるHCl、SOxを反
応吸収し、かつダストも同時に捕集した後、ダス
トおよび反応生成物を分離除去した高温のCaO、
CaCO3と砂との混合物を流動床炉に投入して再
利用するものであるから、安価なCaCO3が利用
できる上に、CaCO3の利用率がきわめて高くな
り、このためランニングコストが安くなり、また
循環して使用するCaCO3と砂との混合物を排ガ
スで加熱して流動床炉に投入するため、熱ロスが
小さくなる、などの効果を有している。 As explained above, the method of the present invention involves introducing CaCO 3 as a desalination/desulfurization agent into a waste incineration fluidized bed furnace, and converting the activated CaO and sand mixture in the furnace into a moving bed type harmful gas. High-temperature CaO is used as a reactant and filter material in duct removal equipment to react and absorb HCl and SOx contained in exhaust gas, and also collect dust at the same time, after which dust and reaction products are separated and removed.
Since the mixture of CaCO 3 and sand is put into a fluidized bed furnace and reused, not only can cheap CaCO 3 be used, but the utilization rate of CaCO 3 is extremely high, which reduces running costs. Furthermore, since the mixture of CaCO 3 and sand that is used in circulation is heated with exhaust gas and then fed into the fluidized bed furnace, it has the effect of reducing heat loss.
図面は本発明の方法を実施する装置の一例を示
す系統的説明図である。
１……流動床炉、２……分離装置、３……移動
層式有害ガス・ダスト除去装置、４……流動媒体
排出装置、５……中間ホツパ、６……余剰CaO・
砂抜出管、７……支持体、８……移動層、１０…
…冷却装置、１１……分離装置、１２……送風
機、１３……サイクロン、１４……空気分散板、
１５……風箱。
The drawing is a systematic explanatory diagram showing an example of an apparatus for carrying out the method of the present invention. 1... Fluidized bed furnace, 2... Separation device, 3... Moving bed harmful gas/dust removal device, 4... Fluidized medium discharge device, 5... Intermediate hopper, 6... Excess CaO.
Sand extraction pipe, 7... Support, 8... Moving layer, 10...
...cooling device, 11 ... separation device, 12 ... blower, 13 ... cyclone, 14 ... air distribution plate,
15...Wind box.
Claims (1)
ス中のHCl、SOxを除去する方法において、流動
床炉内で活性化されたCaO、流動媒体、反応生成
物、不燃物、ダストの混合物を炉底から抜き出
し、反応生成物、不燃物、ダストを分離した後、
CaOおよび流動媒体を移動層式有害ガス・ダスト
除去装置に投入して２枚の支持体間を低速度で落
下させつつ、流動床炉からの排ガスを移動層内に
通過させて、CaOと排ガス中の含有HCl、SOxと
を反応させると同時に排ガス中のダストを捕集し
た後、反応生成物およびダストと、CaCO3、
CaOおよび流動媒体とに分離し、CaCO3、CaO
および流動媒体を流動床炉に供給して発生HCl、
SOxの除去に再利用することを特徴とする廃棄物
焼却炉排ガス中の有害成分・ダスト除去方法。1 In a method of removing HCl and SOx from exhaust gas by introducing limestone into a waste incineration fluidized bed furnace, a mixture of activated CaO, fluidized medium, reaction products, incombustibles, and dust is After extracting from the bottom of the furnace and separating reaction products, incombustibles, and dust,
CaO and a fluidized medium are introduced into a moving bed type noxious gas/dust removal device and are allowed to fall between two supports at low speed, while the exhaust gas from the fluidized bed furnace is passed through the moving bed. After collecting the dust in the exhaust gas at the same time as reacting the HCl and SOx contained in it, the reaction products and dust, CaCO 3 ,
Separates into CaO and fluid medium, CaCO 3 , CaO
and HCl generated by supplying the fluidized medium to the fluidized bed furnace,
A method for removing harmful components and dust from waste incinerator exhaust gas, which is characterized by reuse for removing SOx.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58057278A JPS59183817A (en) | 1983-03-31 | 1983-03-31 | Removal of harmful component and dust in waste gas from waste incinerator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58057278A JPS59183817A (en) | 1983-03-31 | 1983-03-31 | Removal of harmful component and dust in waste gas from waste incinerator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS59183817A JPS59183817A (en) | 1984-10-19 |
| JPS6345852B2 true JPS6345852B2 (en) | 1988-09-12 |
Family
ID=13051066
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58057278A Granted JPS59183817A (en) | 1983-03-31 | 1983-03-31 | Removal of harmful component and dust in waste gas from waste incinerator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS59183817A (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0611376B2 (en) * | 1984-07-25 | 1994-02-16 | バブコツク日立株式会社 | Method for removing sulfur compounds and halogen compounds in exhaust gas |
| JPS62142907A (en) * | 1985-12-18 | 1987-06-26 | Mitsubishi Heavy Ind Ltd | Pulverized coal burner of slag tap type |
| JPS6330729U (en) * | 1986-08-06 | 1988-02-29 | ||
| US5379705A (en) * | 1992-11-11 | 1995-01-10 | Kawasaki Jukogyo Kabushiki Kaisha | Fluidized-bed incinerator |
| JP2977743B2 (en) * | 1995-07-28 | 1999-11-15 | 川崎重工業株式会社 | Plastic waste gasification gas treatment method |
| JP2004108688A (en) * | 2002-09-19 | 2004-04-08 | Hitachi Zosen Corp | Method and apparatus for burning waste mainly composed of organic phosphorus compounds |
| JP4543629B2 (en) * | 2003-07-09 | 2010-09-15 | 株式会社Inax | Exhaust gas treatment apparatus, calcium fluoride recovery method, and fluorine recovery method |
| JP6339360B2 (en) * | 2013-12-19 | 2018-06-06 | 川崎重工業株式会社 | BOILER WITH CORROSION CONTROL DEVICE AND BOILER CORROSION CONTROL METHOD |
| CN110180493B (en) * | 2019-04-17 | 2022-04-19 | 中节能（合肥）可再生能源有限公司 | Active filter material for removing calcium ions, and preparation method and application thereof |
-
1983
- 1983-03-31 JP JP58057278A patent/JPS59183817A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS59183817A (en) | 1984-10-19 |
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