JPH0326095B2 - - Google Patents
Info
- Publication number
- JPH0326095B2 JPH0326095B2 JP58196128A JP19612883A JPH0326095B2 JP H0326095 B2 JPH0326095 B2 JP H0326095B2 JP 58196128 A JP58196128 A JP 58196128A JP 19612883 A JP19612883 A JP 19612883A JP H0326095 B2 JPH0326095 B2 JP H0326095B2
- Authority
- JP
- Japan
- Prior art keywords
- powder
- hcl
- exhaust gas
- reaction
- filter cloth
- 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
- 239000000843 powder Substances 0.000 claims description 36
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 32
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 32
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 32
- 238000006243 chemical reaction Methods 0.000 claims description 30
- 239000007789 gas Substances 0.000 claims description 24
- 238000000034 method Methods 0.000 claims description 21
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 12
- 239000002002 slurry Substances 0.000 claims description 12
- 238000006386 neutralization reaction Methods 0.000 claims description 8
- 238000010521 absorption reaction Methods 0.000 claims description 7
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 6
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 6
- 239000000920 calcium hydroxide Substances 0.000 claims description 6
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 6
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 6
- 230000001737 promoting effect Effects 0.000 claims description 2
- 239000011575 calcium Substances 0.000 description 22
- 239000004744 fabric Substances 0.000 description 15
- 239000000428 dust Substances 0.000 description 12
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 239000005909 Kieselgur Substances 0.000 description 5
- 235000010216 calcium carbonate Nutrition 0.000 description 5
- 239000010451 perlite Substances 0.000 description 5
- 235000019362 perlite Nutrition 0.000 description 5
- 239000002245 particle Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 238000011001 backwashing Methods 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000011812 mixed powder Substances 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- 239000005995 Aluminium silicate Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 235000012211 aluminium silicate Nutrition 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 239000010433 feldspar Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Description
【発明の詳細な説明】
本発明は排ガス中の塩化水素除去方法に関する
ものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for removing hydrogen chloride from exhaust gas.
有害ガスの排出規制強化に伴い、都市ごみ焼却
炉、ガラス熔融炉、アルミ精錬工場さら排出する
塩化水素（以下HClという）の除去が急務となつ
ている。例えば、発生源数の多い都市ごみ焼却炉
では、排ガス中のHClを乾燥方法により除去する
ために、(1)焼却炉内もしくは排ガスダクト内へ消
石灰（以下Ca（OH）2という）又は炭酸カルシウ
ム（以下CaCO3という）の粉末を吹き込みHClを
中和吸収する、(2)Ca（OH）2のスラリーを反応塔
内へ噴霧し、蒸発乾燥しながらHClを中和吸収す
る、方法がとられている。しかし、HClの除去率
としては80〜90％が上限で、これ以上の高い除去
率が要求される場合はこれら乾式方法でのHCl除
去は難しく、湿式スクラバー方法をとらざるを得
なかつた。 With stricter regulations on harmful gas emissions, there is an urgent need to remove hydrogen chloride (hereinafter referred to as HCl) emitted by municipal waste incinerators, glass melting furnaces, and aluminum smelting plants. For example, in municipal waste incinerators, which have many sources, in order to remove HCl from exhaust gas by drying, (1) slaked lime (hereinafter referred to as Ca (OH) 2 ) or calcium carbonate is added into the incinerator or exhaust gas duct; (2) A slurry of Ca(OH) 2 is sprayed into the reaction tower to neutralize and absorb HCl while evaporating and drying. ing. However, the upper limit for the removal rate of HCl is 80-90%, and if a higher removal rate than this is required, it is difficult to remove HCl using these dry methods, and a wet scrubber method has to be used.
乾式方法により高い除去率を得ることができれ
ば、排水処理が必要な湿式スクラバー方法を採用
することもなく、処理が容易となる。 If a high removal rate can be obtained using a dry method, there will be no need to adopt a wet scrubber method that requires wastewater treatment, making treatment easier.
本発明は、高いHCl除去率を得ることのできる
乾式方法を提案することを目的としてなされたも
ので、バグフイルター方式の乾式塩化水素除去法
を採用し、ろ布の目詰り防止、ろ布の破損防
止、ろ布表面に堆積したダストの通気の性能向
上、堆積したダスト逆洗時の剥離性の向上、及
び排ガス中に含まれる着火カーボンによるろ布
焼損防止を図ることにより、上記目的を達成せん
とするものである。 The present invention was made with the purpose of proposing a dry method that can obtain a high HCl removal rate.It adopts a dry hydrogen chloride removal method using a bag filter method, and prevents clogging of the filter cloth. The above objectives are achieved by preventing damage, improving the ventilation performance of dust accumulated on the filter cloth surface, improving the peelability of accumulated dust during backwashing, and preventing filter cloth burnout due to ignited carbon contained in exhaust gas. This is what I am trying to do.
すなわち本発明は、排ガス中の塩化水素を除去
する方法において、消石灰又は炭酸カルシウムの
粉末もしくは消石灰のスラリーを排ガス中に吹込
んでHClを中和吸収したのち、反応助剤粉末を吹
込んでバグフイルター反応塔内で更にHClの中和
吸収を促進させることを特徴とする塩化水素除去
方法に関するものである。 That is, in a method for removing hydrogen chloride from exhaust gas, the present invention involves blowing slaked lime or calcium carbonate powder or slurry of slaked lime into the exhaust gas to neutralize and absorb HCl, and then blowing reaction aid powder to carry out the bag filter reaction. The present invention relates to a method for removing hydrogen chloride characterized by further promoting neutralization and absorption of HCl within a column.
第１図は本発明方法の流れ図である。G1は
HClを含む排ガス、G2は処理ガス、１はCa
（OH）2又はCaCO3粉末によるHClの中和吸収工
程、もしくはCa（OH）2スラリー噴霧によるHCl
中和吸収工程、２は反応助剤粉末供給装置、３は
バグフイルター反応塔を示す。 FIG. 1 is a flowchart of the method of the present invention. G1 is
Exhaust gas containing HCl, G 2 is processing gas, 1 is Ca
HCl neutralization absorption process by (OH) 2 or CaCO3 powder or HCl by Ca(OH) 2 slurry spraying
In the neutralization absorption step, 2 is a reaction aid powder supply device, and 3 is a bag filter reaction tower.
HClを含む排ガス中に吹き込まれたCa（OH）2
又はCaCO3粉末、もしくはCa（OH）2スラリーは
次式によりHClを中和吸収する。 Ca(OH) 2 blown into flue gas containing HCl
Alternatively, CaCO 3 powder or Ca(OH) 2 slurry neutralizes and absorbs HCl according to the following formula.
Ca（OH）2粉末＋2HCl→CaCl2＋H2O (1)
CaCO3粉末＋2HCl→CaCl2＋H2O＋CO2 (2)
Ca（OH）2スラリー＋2HCl→CaCl2＋H2O (3)
使用するCa（OH）2又はCaCO3粉末およびスラリ
ー状にして使うCa（OH）2粉末は、HClとの中和
吸収を効果的に進める意味から100μ以下の粒径、
好ましくは50μ以下の粒径からなる微粉末がよ
い。Ca(OH) 2 powder + 2HCl → CaCl 2 +H 2 O (1) CaCO 3 powder + 2HCl → CaCl 2 +H 2 O + CO 2 (2) Ca(OH) 2 slurry + 2HCl → CaCl 2 + H 2 O (3) Ca used ( OH) 2 or CaCO 3 powder and Ca(OH) 2 powder used in slurry form should have a particle size of 100μ or less to effectively promote neutralization and absorption with HCl.
A fine powder having a particle size of 50 μm or less is preferable.
排ガス中には通常ダストが含まれ、該排ガス中
に吹き込まれたCa（OH）2又はCaCO3と、該排ガ
ス中のHClとの中和吸収による生成物CaCl2とダ
ストがガス中で混合して、バグフイルター反応塔
３へと流れていく。一方、反応助剤粉末をバグフ
イルター反応塔３の前方で排ガス中に均一に吹込
む。この排ガスがバグフイルター反応塔３のろ布
を通過するとき、排ガス中の上記混合ダストと反
応助剤粉末は、第２図に示すように、ろ布１１表
面に逐次堆積していく。堆積した混合ダストと反
応助剤粉末は一定量堆積した後、ろ布１１の逆洗
操作により払い落され、ろ布１１表面が更新され
る。なお第２図中G3は混合ダストと反応助剤粉
末を含む排ガス、１２は反応助剤粉末からなるブ
レコート層、１３は堆積層、１４は反応助剤粉末
を示す。 The exhaust gas usually contains dust, and the dust is mixed in the gas with Ca(OH) 2 or CaCO 3 blown into the exhaust gas and CaCl 2 , a product of neutralization and absorption with HCl in the exhaust gas. Then, it flows into the bag filter reaction tower 3. On the other hand, reaction aid powder is uniformly blown into the exhaust gas in front of the bag filter reaction tower 3. When this exhaust gas passes through the filter cloth of the bag filter reaction tower 3, the mixed dust and reaction aid powder in the exhaust gas are successively deposited on the surface of the filter cloth 11, as shown in FIG. After a certain amount of accumulated mixed dust and reaction aid powder has been accumulated, the filter cloth 11 is brushed off by backwashing, and the surface of the filter cloth 11 is renewed. In FIG. 2, G 3 is an exhaust gas containing mixed dust and reaction aid powder, 12 is a brecoat layer made of reaction aid powder, 13 is a deposited layer, and 14 is reaction aid powder.
なお、本発明方法において、反応助剤粉末とし
ては、かさ密度が小さい、通気性がよい、
吸気してもベトつかない、１〜100μ粒径、好
ましくは10〜50μ粒径のものが適当で例えば、ゼ
オライト、アルミナ、ケイソウ土、パーライト、
活性白土、カオリン、長石、石英等の粉末の中か
ら選ばれ、１種もしくは２種以上の混合粉末とし
て使用する。この粉体の中でも好適なものとして
はゼオライト、ケイソウ土、特に、都市ごみ焼却
炉排ガスを対象とした場合は、ケイソウ土とパー
ライトの混合粉末が安定した機能を示す。パーラ
イトはコスト高であるため、経済性を考慮すれ
ば、ケイソウ土／パーライトの重量比は100〜
１／100好ましくは50〜１とするが適している。 In addition, in the method of the present invention, the reaction aid powder has low bulk density, good air permeability,
Suitable particles are those with a particle size of 1 to 100μ, preferably 10 to 50μ, that do not become sticky even when inhaled, such as zeolite, alumina, diatomaceous earth, perlite, etc.
It is selected from powders of activated clay, kaolin, feldspar, quartz, etc., and is used as one kind or a mixed powder of two or more kinds. Among these powders, zeolite and diatomaceous earth are preferable, and in particular, when the target is exhaust gas from a municipal waste incinerator, a mixed powder of diatomaceous earth and perlite exhibits a stable function. Perlite is expensive, so if economic efficiency is considered, the weight ratio of diatomaceous earth/perlite should be 100~
A value of 1/100, preferably 50 to 1, is suitable.
上記の反応助剤粉末は、後述の実施例の結果、
Ca（OH）2又はCaCO3粉末、Ca（OH）2スラリー吹
込み量の50wt％以下とすることが好ましく、よ
り好ましくは10〜30wt％とすることが好適であ
る。 The above reaction aid powder was obtained as a result of the examples described below.
The amount of Ca(OH) 2 or CaCO 3 powder or Ca(OH) 2 slurry is preferably 50 wt% or less, more preferably 10 to 30 wt%.
なお、Ca（OH）2、CaCO3粉末又はCa（OH）2ス
ラリーの吹込み量は排ガス中のHClとの反応当量
以上とすればよいことは言うまでもない。 It goes without saying that the amount of Ca(OH) 2 , CaCO 3 powder or Ca(OH) 2 slurry blown should be equal to or more than the reaction equivalent with HCl in the exhaust gas.
本発明方法においては、次のような作用、効果
を奏することができる。 In the method of the present invention, the following actions and effects can be achieved.
(1) 前方のHCl中和吸収工程で、中和に関与せず
に残つたCa（OH）2又はCaCO3粉末もしくはCa
（ON）2スラリー乾燥粉末が第２図に示したよ
うに、ろ布１１表面上に堆積し、この堆積層１
３を排ガスG3が通過するとき、更にHClが中
和吸収するため、HClは非常に低い濃度まで除
去されることになる。(1) Ca(OH) 2 or CaCO 3 powder or Ca remaining without participating in neutralization in the previous HCl neutralization absorption process
(ON) 2 The slurry dry powder is deposited on the surface of the filter cloth 11 as shown in Fig. 2, and this deposited layer 1
When the exhaust gas G3 passes through G3 , HCl is further neutralized and absorbed, so HCl is removed to a very low concentration.
(2) ろ布１１表面は、予め反応助剤粉末でプレコ
ード１２しておくことにより、ダストの堆積層
１３はこのプレコート１２上に形成され、直接
ダストが触れることはないので、ろ布１１の目
詰りやダスト付着による破損が防止できる。(2) The surface of the filter cloth 11 is precoated 12 with reaction aid powder in advance, so that the dust deposit layer 13 is formed on this precoat 12 and the dust does not come in direct contact with the surface of the filter cloth 11. This prevents damage caused by clogging and dust adhesion.
(3) ダストの堆積層１３には通気性のよい反応助
剤粉末１４が含まれており、堆積層の通気抵抗
が低く、圧損が小さいので、排風機動力が小さ
くてすむ。(3) The dust accumulation layer 13 contains the reaction aid powder 14 with good air permeability, and the accumulation layer has low ventilation resistance and pressure loss, so the power of the exhaust machine can be small.
(4) また、消石灰又は炭酸カルシウムの粉末、あ
るいは反応助剤の粉末を供給する場合、これら
の粉末がろ布１１表面上に堆積することによつ
て、着火カーボンとろ布１１との直接接触が避
けられるため、ろ布１１の焼損を防止すること
ができる。(4) In addition, when supplying slaked lime or calcium carbonate powder, or reaction aid powder, these powders accumulate on the surface of the filter cloth 11, thereby preventing direct contact between the ignited carbon and the filter cloth 11. Therefore, burnout of the filter cloth 11 can be prevented.
実施例
都市ごみ焼却炉から排出されるHClの除去を下
記条件及び要領で行なつた。Example HCl discharged from a municipal waste incinerator was removed under the following conditions and procedure.
条件；
焼却炉：150T／日
排ガス量：30000Nm3／ｈ
HCl濃度：700ppm
要領；
バグフイルター反応塔の前方でCa（OH）2粉末
を100Kg／ｈ吹込み、ガス滞留時間を５秒とつて
反応塔へ導く一方、バグフイルター反応塔前方
で、反応助剤（ケイソウ土をパーライトを重量比
９：１で混合したもの）10Kg／ｈを吹込んで反応
塔へ送つた。Conditions: Incinerator: 150T/day Exhaust gas amount: 30000Nm 3 /h HCl concentration: 700ppm Procedure: Inject Ca(OH) 2 powder at 100Kg/h in front of the bag filter reaction tower, and react with a gas residence time of 5 seconds. While leading to the tower, 10 kg/h of a reaction aid (a mixture of diatomaceous earth and perlite in a weight ratio of 9:1) was blown into the bag filter in front of the reaction tower and sent to the reaction tower.
結果；
ろ布表面へのダスト堆積量が1.0Kg／m2のとき、
堆積層の圧損は100mmAqで、反応塔出口のHCl濃
度は10ppm、HCl除去率98.6％であつた。Result: When the amount of dust accumulated on the filter cloth surface is 1.0Kg/ m2 ,
The pressure drop in the deposited layer was 100 mmAq, the HCl concentration at the outlet of the reaction tower was 10 ppm, and the HCl removal rate was 98.6%.
なお、反応助剤を吹込まないときの堆積層の圧
損は130mmAqで、反応助剤を含む場合に比べて約
30mmAq大きい圧損であつた。 The pressure drop in the deposited layer when no reaction aid is injected is 130 mmAq, which is approximately 130 mmAq compared to when the reaction aid is included.
There was a large pressure drop of 30mmAq.
また、Ca（OH）2粉末の代りにCaCO3粉末、Ca
（OH）2スラリーを用いても同様の結果が得られ
た。 Also, instead of Ca(OH) 2 powder, CaCO3 powder, Ca
Similar results were obtained using (OH) 2 slurry.
更に、反応助剤吹込み量を種々変えて行つたと
ころ、Ca（OH）2粉末又はCaCO3粉末もしくはCa
（OH）2スラリー吹込み量の50wt％以下、好まし
くは10〜30wt％の範囲が好適であることが確認
された。 Furthermore, by varying the amount of reaction aid injected, Ca(OH) 2 powder, CaCO 3 powder, or Ca
It was confirmed that the amount of (OH) 2 slurry injected is preferably 50 wt% or less, preferably in the range of 10 to 30 wt%.
第１図は本発明方法の流れ図、第２図は本発明
方法に係るバグフイルターのろ布表面状況の一例
を示す図である。
FIG. 1 is a flowchart of the method of the present invention, and FIG. 2 is a diagram showing an example of the surface condition of the filter cloth of a bag filter according to the method of the present invention.
Claims (1)
て、消石灰又は炭酸カルシウムの粉末もしくは消
石灰のスラリーを排ガス中に吹込んでHClを中和
吸収したのち、反応助剤粉末を吹込んでバグフイ
ルター反応塔内で更にHClの中和吸収を促進させ
ることを特徴とする塩化水素除去方法。1 In a method for removing hydrogen chloride from exhaust gas, slaked lime or calcium carbonate powder or slaked lime slurry is injected into the exhaust gas to neutralize and absorb HCl, and then a reaction aid powder is blown in to further remove it in a bag filter reaction tower. A hydrogen chloride removal method characterized by promoting neutralization absorption of HCl.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58196128A JPS6090028A (en) | 1983-10-21 | 1983-10-21 | Removing method of hydrogen chloride |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58196128A JPS6090028A (en) | 1983-10-21 | 1983-10-21 | Removing method of hydrogen chloride |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6090028A JPS6090028A (en) | 1985-05-21 |
| JPH0326095B2 true JPH0326095B2 (en) | 1991-04-09 |
Family
ID=16352706
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58196128A Granted JPS6090028A (en) | 1983-10-21 | 1983-10-21 | Removing method of hydrogen chloride |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6090028A (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0757305B2 (en) * | 1990-12-28 | 1995-06-21 | 日立造船株式会社 | Treatment method of exhaust gas containing hydrogen chloride |
| JP2003093837A (en) * | 2001-09-26 | 2003-04-02 | Okutama Kogyo Co Ltd | Exhaust gas treatment agent |
| CN102989115B (en) * | 2012-11-05 | 2014-07-30 | 总装备部工程设计研究总院 | Alkaline powder for treating leaked nitric acid and volatile toxic gases of nitric acid and production method of alkaline powder |
| CN102989113B (en) * | 2012-11-05 | 2014-08-06 | 总装备部工程设计研究总院 | Alkaline powder for treating leaked hydrochloric acid and acid mist thereof and preparation method of alkaline powder |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS48108064U (en) * | 1972-03-17 | 1973-12-13 | ||
| JPS5253620U (en) * | 1975-10-14 | 1977-04-18 | ||
| JPS593150Y2 (en) * | 1979-10-30 | 1984-01-28 | 横浜ゴム株式会社 | Clamp device for turbocharger |
-
1983
- 1983-10-21 JP JP58196128A patent/JPS6090028A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6090028A (en) | 1985-05-21 |
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