JPH11114366A - Treatment of released gas in waste gas treating device for refuse incinerator - Google Patents
Treatment of released gas in waste gas treating device for refuse incineratorInfo
- Publication number
- JPH11114366A JPH11114366A JP9268745A JP26874597A JPH11114366A JP H11114366 A JPH11114366 A JP H11114366A JP 9268745 A JP9268745 A JP 9268745A JP 26874597 A JP26874597 A JP 26874597A JP H11114366 A JPH11114366 A JP H11114366A
- Authority
- JP
- Japan
- Prior art keywords
- activated carbon
- exhaust gas
- lime
- desorbed
- dioxin
- 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
- 239000007789 gas Substances 0.000 title abstract description 49
- 239000002912 waste gas Substances 0.000 title abstract 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 53
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 24
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 24
- 239000004571 lime Substances 0.000 claims abstract description 24
- 239000007921 spray Substances 0.000 claims abstract description 18
- 239000000428 dust Substances 0.000 claims abstract description 13
- 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 claims abstract description 12
- 238000001179 sorption measurement Methods 0.000 claims abstract description 11
- 150000003839 salts Chemical class 0.000 claims abstract description 4
- 238000003795 desorption Methods 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims 1
- 229910017917 NH4 Cl Inorganic materials 0.000 abstract 1
- 238000010438 heat treatment Methods 0.000 abstract 1
- 238000010612 desalination reaction Methods 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Treating Waste Gases (AREA)
- Filtering Of Dispersed Particles In Gases (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明はゴミ焼却炉の排ガス
処理装置における脱離ガス処理方法に関するものであ
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for treating desorbed gas in an exhaust gas treatment device of a refuse incinerator.
【０００２】[0002]
【従来の技術】排ガス処理装置の脱離ガスは通常洗浄し
て回収するのが普通であるが、ごみ焼却炉の排ガス中の
ＳＯ2の濃度は０〜５０ppmと少ない。これを回収する為
に莫大な費用を投資することは不合理である。 2. Description of the Related Art Desorption gas from an exhaust gas treatment device is usually washed and recovered, but the concentration of SO 2 in exhaust gas from a refuse incinerator is as low as 0 to 50 ppm. It is irrational to invest a huge amount of money to recover this.
【０００３】従来は、脱離ガスを洗浄して、清浄なＳＯ
2ガスとし、硫酸等として回収していた。しかし、上述
したとおり、ゴミ焼却炉の場合はＳＯ2の濃度が低く、
さらにＳＯ2の濃度が一定でなく変動する。従って、脱
離ガス一定の運転が不可能であるので、硫酸回収やその
他の回収装置をつけることが困難であった。[0003] Conventionally, desorbed gas is cleaned to obtain a clean SO
It was recovered as two gases and sulfuric acid. However, as described above, in the case of a garbage incinerator, the concentration of SO 2 is low,
Furthermore, the concentration of SO 2 is not constant and fluctuates. Therefore, since it is impossible to perform a constant operation of the desorbed gas, it has been difficult to attach sulfuric acid and other recovery devices.
【０００４】[0004]
【発明が解決しようとする課題】本発明に係る脱離ガス
処理方法は、脱離ガス中にはＳＯ2とＨＣl及び少量のＮ
Ｈ3を含んでいることを利用し、排ガス処理装置の前段
に設けた脱塩用の石灰噴霧塔の前に脱離ガスを戻すこと
により新たな設備を設置しないで脱離ガスを回収するこ
とを課題とする。According to the desorption gas treatment method of the present invention, the desorption gas contains SO 2 and HCl and a small amount of N 2.
Utilizing the fact that it contains H 3 , recovering desorbed gas without installing new equipment by returning desorbed gas in front of a lime spray tower for desalination installed upstream of an exhaust gas treatment device As an issue.
【０００５】[0005]
【課題を解決するための手段】本発明に係る脱離ガス処
理装置は、ボイラ出口に石灰噴霧塔が設けられ、排ガス
はこの石灰噴霧塔で所定の塩濃度迄下げられ、噴霧され
た石灰は電気集じん器又はバグフィルタによりアッシュ
（灰）と共に捕集され、次に、ブロアを介して熱交換器
により排ガス温度を所定の制御温度の範囲に制御して吸
着塔に導き、吸着塔には粒状の活性炭を充填し、移動さ
せ、排ガスは活性炭と接触させたのち煙突へ放出するゴ
ミ焼却炉の排ガス処理装置において、ＳＯ2及びダイオ
キシンは粒状の活性炭に吸着し、ＮＯxは熱交換器の後
段から煙道に注入したＮＨ3の存在で分解し、一部はＮ
Ｈ4Ｃlとしてダストと共に吸着塔の活性炭層で濾過集じ
んされ、さらに、ＳＯ2、ダイオキシン及びＨＣlを吸着
した粒状の活性炭は脱離塔に導かれ、加熱してＳＯ2を
脱離、ダイオキシンを分解、ＨＣlを脱離し、脱離再生
された活性炭は冷却され脱離塔から排出され、そして、
脱離ガスは石灰噴霧塔の前段に戻され、排ガスと共に脱
塩され、ＳＯ2も噴霧された石灰で固定されるようにし
たことを特徴とする。In the desorption gas treatment apparatus according to the present invention, a lime spray tower is provided at a boiler outlet, and exhaust gas is reduced to a predetermined salt concentration by the lime spray tower. The ash is collected together with the ash by an electric dust collector or a bag filter, and then the exhaust gas temperature is controlled to a predetermined control temperature range by a heat exchanger through a blower and guided to an adsorption tower. the granular activated carbon was filled, is moved, the exhaust gas in the exhaust gas treatment apparatus of the refuse incinerator to release the chimney after contacted with activated carbon, SO 2 and dioxin adsorbed to the granular activated carbon, NOx subsequent stage of the heat exchanger Decomposed in the presence of NH 3 injected into the flue from
H 4 Cl is filtered and collected together with the dust in the activated carbon layer of the adsorption tower, and the granular activated carbon adsorbing SO 2 , dioxin and HCl is led to the desorption tower, where it is heated to desorb SO 2 and dioxin is removed. The activated carbon decomposed, desorbed HCl, desorbed and regenerated, was cooled and discharged from the desorption tower, and
The desorbed gas is returned to the preceding stage of the lime spray tower, is desalted together with the exhaust gas, and SO 2 is fixed by the sprayed lime.
【０００６】[0006]
【発明の実施の形態】本発明の実施の形態を図面を参照
して説明する。図１に示す排ガス処理装置は、ボイラ出
口に脱塩用の石灰噴霧塔が設けられ、排ガスはこの噴霧
塔で所定の塩濃度迄下げられ、噴霧された石灰は電気集
じん器又はバグフィルタによりアッシュ（灰）と共に捕
集される。Embodiments of the present invention will be described with reference to the drawings. The exhaust gas treatment apparatus shown in FIG. 1 is provided with a lime spray tower for desalination at the boiler outlet, the exhaust gas is lowered to a predetermined salt concentration by this spray tower, and the sprayed lime is collected by an electric dust collector or a bag filter. Collected with ash.
【０００７】次に、ブロアを介して熱交換器により排ガ
ス温度を所定の制御温度（例えば１２０℃〜１６０℃）
迄下げ、吸着塔に導く。吸着塔には粒状の活性炭を充填
し、移動する方式とする。排ガスは活性炭と接触したの
ち煙突へ放出する。Next, the exhaust gas temperature is controlled by a heat exchanger through a blower to a predetermined control temperature (for example, 120 ° C. to 160 ° C.).
To the adsorption tower. The adsorption tower is packed with granular activated carbon and moved. The exhaust gas is released into the chimney after contacting the activated carbon.
【０００８】ＳＯ2及びダイオキシンは粒状の活性炭に
吸着し、ＮＯxは熱交換器の後段から煙道に注入したＮ
Ｈ3の存在で分解する。一部はＮＨ4Ｃlとしてダストと
共に吸着塔の活性炭層で濾過集じんされる。[0008] SO 2 and dioxin are adsorbed on the granular activated carbon, and NOx is discharged from the latter part of the heat exchanger into N 2 injected into the flue.
Decomposes in the presence of H 3 . A part is collected by filtration in the activated carbon layer of the adsorption tower together with dust as NH 4 Cl.
【０００９】ＳＯ2、ダイオキシン及びＨＣlを吸着した
粒状の活性炭は脱離塔に導かれ、加熱してＳＯ2を脱
離、ダイオキシンを分解、ＨＣlを脱離する。脱離再生
された活性炭は冷却され脱離塔から排出される。The granular activated carbon having adsorbed SO 2 , dioxin and HCl is led to a desorption tower, where it is heated to desorb SO 2 , decompose dioxin, and desorb HCl. The activated carbon desorbed and regenerated is cooled and discharged from the desorption tower.
【００１０】脱離塔下の筋分け機で粉塵と活性炭粉を分
離し、粒状の活性炭は吸着塔に戻され、再使用するため
に循環させる。脱離ガスは脱塩用の石灰噴霧塔の前段に
戻され、メインの排ガスと共に脱塩され、ＳＯ2も噴霧
された石灰で固定される。粉塵は炉に戻して燃焼させる
か、又は脱塩用の石灰噴霧塔に入れる。Dust and activated carbon powder are separated by a separating machine below the desorption tower, and the granular activated carbon is returned to the adsorption tower and circulated for reuse. The desorbed gas is returned to the previous stage of the lime spray tower for desalination, is desalted together with the main exhaust gas, and SO 2 is also fixed by the sprayed lime. The dust is returned to the furnace for combustion or placed in a lime spray tower for desalination.
【００１１】図２及び図３は、既設のゴミ焼却炉に上記
プロセスを増設する例であり、図２は集じんをバグフィ
ルタにより行う従来の排ガス処理装置に増設プロセスを
付加した例であり、図３は集じんを電気集じん器により
行う従来の排ガス処理装置に増設プロセスを付加した例
である。いずれも、上述した本発明に係る排ガス処理装
置と同等の作用を奏するものである。FIGS. 2 and 3 show an example in which the above process is added to an existing refuse incinerator, and FIG. 2 shows an example in which an additional process is added to a conventional exhaust gas treatment apparatus that performs dust collection using a bag filter. FIG. 3 shows an example in which an additional process is added to a conventional exhaust gas treatment apparatus that performs dust collection using an electric dust collector. In any case, the same effects as those of the above-described exhaust gas treatment apparatus according to the present invention can be obtained.
【００１２】上述したように、脱離塔から出た脱離ガス
を石灰噴霧塔前の煙道に戻す。脱離ガスは、排ガス処理
装置の処理ガス量の１％以下である。又脱離ガス濃度は
向流時（脱離ガスと活性炭の流れが）の時で１８０℃以
上、並流時のとき３００〜３５０℃であるが、少量なの
で石灰噴霧塔の前段に戻すことにより、排ガス温度とほ
ぼ同じ温度で脱塩処理がなされる。[0012] As described above, the desorbed gas discharged from the desorption tower is returned to the flue in front of the lime spray tower. The desorbed gas is 1% or less of the processing gas amount of the exhaust gas processing device. The concentration of desorbed gas is 180 ° C or more during countercurrent flow (flow of desorbed gas and activated carbon), and 300 to 350 ° C when cocurrent, but since it is a small amount, it can be returned to the previous stage of the lime spray tower. The desalination is performed at substantially the same temperature as the exhaust gas temperature.
【００１３】なお、脱離ガスを石灰噴霧塔の前段に戻す
ことにより、脱離ガスの成分であるＨＣl，ＳＯ2等は、 ２ＨＣl＋ＣaＯ→ＣaＣl2＋Ｈ2Ｏ ２ＨＣl＋Ｃa(ＯＨ)2→ＣaＣl2＋２Ｈ2Ｏ ＳＯ2＋ＣaＯ＋(１／２)Ｏ2→ＣaＳＯ4 ＳＯ2＋Ｃa(ＯＨ)2＋(１／２)Ｏ2→ＣaＳＯ4＋Ｈ2Ｏ ＨＣl＋ＮＨ3→ＮＨ4Ｃl 等の反応が進行することにより処理される。By returning the desorbed gas to the preceding stage of the lime spray tower, the components of the desorbed gas, such as HCl and SO 2, are 2HCl + CaO → CaCl 2 + H 2 O 2HCl + Ca (OH) 2 → CaCl 2 + 2H 2 Processed by the progress of a reaction such as OSO 2 + CaO + (1/2) O 2 → CaSO 4 SO 2 + Ca (OH) 2 + (1/2) O 2 → CaSO 4 + H 2 O HCl + NH 3 → NH 4 Cl Is done.
【００１４】[0014]
【発明の効果】本発明に係る脱離ガス処理方法によれ
ば、脱離ガスの回収装置を新たに設置する必要はなく、
脱離ガスを石灰噴霧塔の入口煙道(前後)に戻すだけで、
既存の石灰噴霧塔でメインの排ガスと共に処理すること
ができる。According to the desorbed gas treatment method of the present invention, it is not necessary to newly install a desorbed gas recovery device.
Just return the desorbed gas to the entrance flue (front and back) of the lime spray tower,
The existing lime spray tower can be processed together with the main exhaust gas.
【図１】本発明に係るゴミ焼却炉における排ガス処理装
置の概略構成図。FIG. 1 is a schematic configuration diagram of an exhaust gas treatment device in a refuse incinerator according to the present invention.
【図２】従来の排ガス処理装置に増設プロセスを付加し
た例を示す概略構成図。FIG. 2 is a schematic configuration diagram showing an example in which an additional process is added to a conventional exhaust gas treatment device.
【図３】従来の排ガス処理装置に増設プロセスを付加し
た例を示す概略構成図。FIG. 3 is a schematic configuration diagram showing an example in which an additional process is added to a conventional exhaust gas treatment device.
─────────────────────────────────────────────────────
────────────────────────────────────────────────── ───
【手続補正書】[Procedure amendment]
【提出日】平成９年１０月１７日[Submission date] October 17, 1997
【手続補正１】[Procedure amendment 1]
【補正対象書類名】図面[Document name to be amended] Drawing
【補正対象項目名】全図[Correction target item name] All figures
【補正方法】変更[Correction method] Change
【補正内容】[Correction contents]
【図１】 FIG.
【図２】 FIG. 2
【図３】 FIG. 3
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 ＦＩ Ｂ０１Ｄ 53/70 Ｂ０１Ｄ 53/34 １３４Ａ 53/68 ──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. 6 Identification code FI B01D 53/70 B01D 53/34 134A 53/68
Claims (1)
ガスはこの石灰噴霧塔で所定の塩濃度迄下げられ、噴霧
された石灰は電気集じん器又はバグフィルタによりアッ
シュ（灰）と共に捕集され、次に、ブロアを介して熱交
換器により排ガス温度を所定の制御温度の範囲に制御し
て吸着塔に導き、吸着塔には粒状の活性炭を充填し、移
動させ、排ガスは活性炭と接触させたのち煙突へ放出す
るゴミ焼却炉の排ガス処理装置において、ＳＯ2及びダ
イオキシンは粒状の活性炭に吸着し、ＮＯxは熱交換器
の後段から煙道に注入したＮＨ3の存在で分解し、一部
はＮＨ4Ｃlとしてダストと共に吸着塔の活性炭層で濾過
集じんされ、さらに、ＳＯ2、ダイオキシン及びＨＣlを
吸着した粒状の活性炭は脱離塔に導かれ、加熱してＳＯ
2を脱離、ダイオキシンを分解、ＨＣlを脱離し、脱離再
生された活性炭は冷却され脱離塔から排出され、そし
て、脱離ガスは石灰噴霧塔の前段に戻され、排ガスと共
に脱塩され、ＳＯ2も噴霧された石灰で固定されるよう
にしたことを特徴とするゴミ焼却炉の排ガス処理装置に
おける脱離ガス処理方法。1. A lime spray tower is provided at an outlet of a boiler, exhaust gas is reduced to a predetermined salt concentration by the lime spray tower, and the sprayed lime is collected together with ash (ash) by an electric dust collector or a bag filter. Then, the exhaust gas temperature is controlled to a predetermined control temperature range by a heat exchanger through a blower and guided to an adsorption tower, and the adsorption tower is filled with granular activated carbon and moved, and the exhaust gas contacts the activated carbon. in the exhaust gas treatment apparatus of the refuse incinerator to release the chimney mixture was allowed to, SO 2 and dioxin adsorbed to the granular activated carbon, NOx is decomposed in the presence of NH 3 injected into the flue from the latter stage of the heat exchanger, one The part is filtered and collected as NH 4 Cl together with the dust in the activated carbon layer of the adsorption tower, and the granular activated carbon adsorbing SO 2 , dioxin and HCl is led to the desorption tower and heated to remove SO 2.
2 is desorbed, dioxin is decomposed, HCl is desorbed, the desorbed and regenerated activated carbon is cooled and discharged from the desorption tower, and the desorbed gas is returned to the previous stage of the lime spray tower and is desalted together with the exhaust gas. desorbed gas treatment method in the exhaust gas treatment apparatus of refuse incinerators, characterized in that it has to be fixed by the sO 2 was also sprayed lime.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP26874597A JP3411484B2 (en) | 1997-10-01 | 1997-10-01 | Desorption gas treatment method in exhaust gas treatment equipment of garbage incinerator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP26874597A JP3411484B2 (en) | 1997-10-01 | 1997-10-01 | Desorption gas treatment method in exhaust gas treatment equipment of garbage incinerator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH11114366A true JPH11114366A (en) | 1999-04-27 |
| JP3411484B2 JP3411484B2 (en) | 2003-06-03 |
Family
ID=17462756
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP26874597A Expired - Fee Related JP3411484B2 (en) | 1997-10-01 | 1997-10-01 | Desorption gas treatment method in exhaust gas treatment equipment of garbage incinerator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3411484B2 (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006064836A1 (en) * | 2004-12-15 | 2006-06-22 | Sintokogio, Ltd. | Method and apparatus for treatment of exhaust gas |
| CN101310835B (en) | 2008-02-22 | 2011-01-12 | 重庆钢铁集团设计院 | Semi-dry waste incineration flue gas purification treatment method and system |
| CN103721484A (en) * | 2012-10-15 | 2014-04-16 | 北京博朗环境工程技术股份有限公司 | Semi-dry flue gas purification technology for synergistic removal of various pollutants by coaxial short-range rapid circulation |
| CN105148696A (en) * | 2015-08-11 | 2015-12-16 | 南京中电环保科技有限公司 | Denitration and dust removal system and method for industrial kiln gas |
| CN106823651A (en) * | 2017-02-21 | 2017-06-13 | 中山市道享节能技术服务有限公司 | A high-efficiency composite dust collector |
| CN108392956A (en) * | 2017-02-05 | 2018-08-14 | 鞍钢股份有限公司 | Desulfurization and denitrification system and method for coke oven flue gas |
| CN109603538A (en) * | 2019-01-22 | 2019-04-12 | 山东景耀玻璃集团有限公司 | Integrated comprehensive technology for waste heat recovery of kiln exhaust gas desulfurization, denitrification and dust removal |
| CN109794135A (en) * | 2019-01-15 | 2019-05-24 | 北京科技大学 | Adsorption, removal and resource utilization of multi-pollutants in flue gas based on waste heat utilization |
| CN111013343A (en) * | 2019-12-17 | 2020-04-17 | 无锡市华星东方电力环保科技有限公司 | Waste incineration system |
| CN113509827A (en) * | 2021-04-19 | 2021-10-19 | 中冶长天国际工程有限责任公司 | Temperature control method in sintering flue gas multi-pollutant treatment process |
| CN115212691A (en) * | 2021-04-19 | 2022-10-21 | 中冶长天国际工程有限责任公司 | A desorption method and desorption tower for activated carbon adsorbing pollutants in flue gas |
-
1997
- 1997-10-01 JP JP26874597A patent/JP3411484B2/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006064836A1 (en) * | 2004-12-15 | 2006-06-22 | Sintokogio, Ltd. | Method and apparatus for treatment of exhaust gas |
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| CN113509827A (en) * | 2021-04-19 | 2021-10-19 | 中冶长天国际工程有限责任公司 | Temperature control method in sintering flue gas multi-pollutant treatment process |
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