JPH08108038A - Fly ash waste gas neutralization treating method - Google Patents
Fly ash waste gas neutralization treating methodInfo
- Publication number
- JPH08108038A JPH08108038A JP24761794A JP24761794A JPH08108038A JP H08108038 A JPH08108038 A JP H08108038A JP 24761794 A JP24761794 A JP 24761794A JP 24761794 A JP24761794 A JP 24761794A JP H08108038 A JPH08108038 A JP H08108038A
- Authority
- JP
- Japan
- Prior art keywords
- fly ash
- calcium carbonate
- exhaust gas
- tank
- blowing nozzle
- 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.)
- Withdrawn
Links
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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/20—Waste processing or separation
Landscapes
- Treating Waste Gases (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、ゴミ焼却炉の排ガス等
に含まれる飛灰を炭酸ガスを含む排ガスで中和する飛灰
の排ガス中和処理方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for neutralizing fly ash by means of neutralizing fly ash contained in exhaust gas of a refuse incinerator with exhaust gas containing carbon dioxide.
【０００２】[0002]
【従来の技術】従来の飛灰の排ガス中和処理方法を、図
３によって説明する。灰汚水を灰汚水槽３より図示しな
いポンプで取り出し、集塵装置で捕集されたごみ焼却炉
の排ガス中の飛灰１が供給される飛灰溶解槽２に前記灰
汚泥水を送って飛灰１を溶解させている。この飛灰１を
溶解した水を飛灰無害化槽４に送り、集塵装置を出たご
み焼却炉の排ガス５を排ガス供給ファン１１によって飛
灰無害化槽４内へ導入し、排ガス５に含まれる炭酸ガス
（ＣＯ2 ）によって飛灰１中に含まれるカルシウム等の
未反応のアルカリ分を中和する。その上で排ガス５はご
み焼却炉の炉内１２に戻される。前記未反応のアルカリ
分の炭酸ガスによる中和によって、飛灰無害化槽４内に
おいて炭酸カルシウム（ＣａＣＯ3 ）等が生成される。2. Description of the Related Art A conventional method for neutralizing exhaust gas from fly ash will be described with reference to FIG. Ash sewage is taken out of the ash sewage tank 3 by a pump (not shown), and the ash sludge water is sent to the fly ash dissolution tank 2 to which the fly ash 1 in the exhaust gas of the refuse incinerator collected by the dust collector is supplied. Ash 1 is dissolved. The water in which the fly ash 1 is dissolved is sent to the fly ash detoxification tank 4, and the exhaust gas 5 of the refuse incinerator that has left the dust collector is introduced into the fly ash detoxification tank 4 by the exhaust gas supply fan 11 to form the exhaust gas 5. Carbon dioxide gas (CO 2 ) contained neutralizes unreacted alkali components such as calcium contained in the fly ash 1. Then, the exhaust gas 5 is returned to the inside 12 of the refuse incinerator. Neutralization of the unreacted alkali content with carbon dioxide produces calcium carbonate (CaCO 3 ) in the fly ash detoxification tank 4.
【０００３】このようにして中和処理を受けた飛灰１を
溶解した水は、飛灰無害化槽４から飛灰汚泥濃縮槽６へ
送られて濃縮される。この際、炭酸カルシウムは固形物
であるので沈降し、沈降した炭酸カルシウムのスラリー
は飛灰汚泥濃縮槽６の底部より飛灰汚泥移送ポンプ７に
より脱水機汚泥供給配管２１を経て脱水機８へ送られ、
脱水汚泥９として飛灰ホッパ１０に貯留され、同飛灰ホ
ッパ１０からトラック１９によって搬出される。The water in which the fly ash 1 thus neutralized is dissolved is sent from the fly ash detoxification tank 4 to the fly ash sludge concentrating tank 6 for concentration. At this time, since calcium carbonate is a solid substance, it settles, and the settled calcium carbonate slurry is sent to the dehydrator 8 from the bottom of the fly ash sludge concentrating tank 6 by the fly ash sludge transfer pump 7 through the dehydrator sludge supply pipe 21. The
The dewatered sludge 9 is stored in the fly ash hopper 10 and is carried out from the fly ash hopper 10 by the truck 19.
【０００４】一方、飛灰汚泥濃縮槽６で炭酸カルシウム
が分離された飛灰１を溶解した水は、灰沈でん槽１８で
飛灰が沈でんされた上同灰沈でん槽１８をオーバーフロ
ーして隣接して設けられた汚泥水槽３内に灰汚水として
貯留される。この灰汚水は、灰汚水処理装置２０で処理
された上放水されるが、その一部は前記のように飛灰溶
解槽２に送られて飛灰１の溶解に使用される。On the other hand, the water in which the fly ash 1 from which calcium carbonate has been separated in the fly ash sludge concentrating tank 6 is dissolved overflows the upper ash settling tank 18 in which the fly ash has been settled in the ash settling tank 18 and is adjacent to it. It is stored as ash wastewater in the sludge water tank 3 provided as above. The ash sewage is treated by the ash sewage treatment apparatus 20 and then discharged, and a part of the ash sewage is sent to the fly ash dissolution tank 2 and used to dissolve the fly ash 1 as described above.
【０００５】なお、２ａ，４ａはそれぞれ飛灰溶解槽２
と飛灰無害化槽４に設けられたモータで駆動される攪拌
機である。2a and 4a are fly ash dissolution tanks 2 respectively.
And a stirrer driven by a motor provided in the fly ash detoxification tank 4.
【０００６】前記飛灰無害化槽４内には、図４に示すよ
うに、排ガス供給ファン１１からの排ガス５が流れその
先端部１４から排ガス５を吹き込む吹き出しノズル１３
と飛灰溶解槽２からの飛灰１を溶解した水が供給される
配管１６が設けられ、また同槽４には前記中和処理を行
った排ガス５をごみ焼却炉の炉内１２へ戻す出口ノズル
１７が設けられている。As shown in FIG. 4, in the fly ash detoxification tank 4, the exhaust gas 5 from the exhaust gas supply fan 11 flows and the exhaust nozzle 5 blows the exhaust gas 5 from the tip portion 14 thereof.
And a pipe 16 to which water in which the fly ash 1 is dissolved from the fly ash dissolution tank 2 is supplied, and the exhaust gas 5 which has been subjected to the neutralization process is returned to the furnace interior 12 of the refuse incinerator in the same tank 4. An outlet nozzle 17 is provided.
【０００７】また、飛灰無害化槽４では、排ガス５の吹
き出しノズル１３の先端部１４に炭酸カルシウムのスケ
ールが析出するために、攪拌機４ａによって槽内の液を
攪拌し、液の濃度の平均化を図っている。Further, in the fly ash detoxification tank 4, since calcium carbonate scale is deposited on the tip portion 14 of the blowing nozzle 13 for the exhaust gas 5, the liquid in the tank is agitated by the agitator 4a, and the average concentration of the liquid is averaged. It is trying to make it.
【０００８】[0008]
【発明が解決しようとする課題】前記の図３及び図４に
示す従来の飛灰の排ガス中和処理方法における飛灰無害
化槽４では、排ガス５中の炭酸ガスによって飛灰１中の
未反応アルカリ分を中和しているが、炭酸カルシウム
は、 Ｃａ（ＯＨ）2 ＋ＣＯ2 →ＣａＣＯ3 の反応によって生成される。In the fly ash detoxification tank 4 in the conventional fly ash exhaust gas neutralization treatment method shown in FIG. 3 and FIG. Although the reaction alkali content is neutralized, calcium carbonate is produced by the reaction of Ca (OH) 2 + CO 2 → CaCO 3 .
【０００９】炭酸ガスを含む排ガス５を吹き込む飛灰無
害化槽４の吹き出しノズル１３の先端部１４の近傍は、
単位体積当りの炭酸カルシウムの生成量〔ｋｇ−ｍｏｌ
／ｍ 3 ・ｈｒ〕が大きくなり、その結果、吹き出しノズ
ル１３の先端部１４の近傍では過飽和度（溶解炭酸カル
シウム／飽和炭酸カルシウム）が上昇し、炭酸カルシウ
ムのスケールが析出して同先端部１４に付着する。No fly ash blown with the exhaust gas 5 containing carbon dioxide
The vicinity of the tip portion 14 of the blowing nozzle 13 of the poisoning tank 4 is
Amount of calcium carbonate produced per unit volume [kg-mol
/ M 3・ Hr] becomes large, and as a result
The degree of supersaturation (dissolved calcium carbonate)
Calcium / saturated calcium carbonate) rises and calcium carbonate
The scale of the metal is deposited and adheres to the tip portion 14.
【００１０】析出した炭酸カルシウムが吹き込みノズル
１３に付着することを防止するために、前記従来の飛灰
の排ガス中和処理方法では、図４に示すように、飛灰無
害化槽４に攪拌機４ａを設けて槽内の液を攪拌し、液の
濃度の平均化を図っている。しかし、このような攪拌を
行っても、吹き出しノズル１３の先端部１４での炭酸カ
ルシウムの局部的な高濃度化を充分に緩和することがで
きず、炭酸カルシウムのスケールが吹き出しノズル１３
の先端部１４に付着して吹き出しノズル１３の閉塞が発
生を防止することができないという問題点があった。In order to prevent the precipitated calcium carbonate from adhering to the blow-in nozzle 13, the conventional fly ash exhaust gas neutralization treatment method uses a stirrer 4a in the fly ash detoxification tank 4 as shown in FIG. Is provided to stir the liquid in the tank so that the concentration of the liquid is averaged. However, even if such stirring is performed, it is not possible to sufficiently mitigate the local increase in the concentration of calcium carbonate at the tip portion 14 of the blowing nozzle 13, and the scale of calcium carbonate may be removed.
There is a problem that it is impossible to prevent the clogging of the blowing nozzle 13 by being attached to the tip portion 14 of the above.
【００１１】本発明は、以上の問題点を解決することが
できる飛灰の排ガス中和処理方法を提供しようとするも
のである。The present invention intends to provide a method for neutralizing fly ash by means of exhaust gas, which can solve the above problems.
【００１２】[0012]
【課題を解決するための手段】本発明は、飛灰を溶解し
た水を収容した飛灰無害化槽に炭酸ガスを含む排ガスを
吹き出しノズルより吹き込んで飛灰中に含まれる未反応
アルカリ分を中和する飛灰の排ガス中和処理方法におい
て、前記中和によって生成された炭酸カルシウムを濃縮
した上種晶として前記飛灰無害化槽へ再循環させて、前
記排ガスの吹き出しノズルへの炭酸カルシウムのスケー
ルの付着を防止するようにした。According to the present invention, an unreacted alkali component contained in fly ash is blown into a fly ash detoxification tank containing water in which fly ash is dissolved by blowing exhaust gas containing carbon dioxide gas from a blowing nozzle. In the method for neutralizing fly ash by exhaust gas neutralization, the calcium carbonate produced by the neutralization is recirculated to the fly ash detoxification tank as concentrated seed crystals, and calcium carbonate is blown to the exhaust gas blowing nozzle. The scale was prevented from adhering.
【００１３】[0013]
【作用】本発明では、飛灰無害化槽において排ガスに含
まれる炭酸ガスによって飛灰中に含まれる未反応アルカ
リ分を中和する際に生成される炭酸カルシウムを濃縮し
た上、種晶として飛灰無害化槽に再循環させる。これに
よって、スケールの種晶となる炭酸カルシウムの液中濃
度が高められて犠牲面としての炭酸カルシウムの表面積
が増大し、吹き出しノズルの近傍における炭酸カルシウ
ムの過飽和度を下げてスケールの析出を緩和することが
できる。その結果、吹き出しノズルへ炭酸カルシウムが
スケールとして付着することを防止することができる。In the present invention, in the fly ash detoxification tank, the calcium carbonate produced when the unreacted alkali component contained in the fly ash is neutralized by the carbon dioxide gas contained in the exhaust gas is concentrated, and the fly ash is dispersed as seed crystals. Recycle to ash detoxification tank. As a result, the concentration of calcium carbonate, which is a seed crystal of the scale, in the liquid is increased, the surface area of calcium carbonate as a sacrificial surface is increased, and the degree of supersaturation of calcium carbonate in the vicinity of the blowing nozzle is reduced to reduce scale precipitation. be able to. As a result, it is possible to prevent calcium carbonate from adhering to the blowing nozzle as scale.
【００１４】[0014]
【実施例】本発明の一実施例を、図１及び図２によって
説明する。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the present invention will be described with reference to FIGS.
【００１５】本実施例は、図３及び図４に示す従来の飛
灰の排ガス中和処理方法を以下説明するように改良した
ものであり、図１及び図２において図３及び図４に示す
部分と同一の部分には同一の符号を付し、その説明を省
略する。This embodiment is an improvement of the conventional fly ash exhaust gas neutralization treatment method shown in FIGS. 3 and 4 as described below, and is shown in FIGS. 3 and 4 in FIGS. 1 and 2. The same parts as the parts are designated by the same reference numerals, and the description thereof will be omitted.
【００１６】即ち、本実施例では、図１及び図２に示す
ように、脱水汚泥供給配管２１の弁２２より上流側の部
分より種晶戻し配管１５が分岐しており、同種晶戻し配
管１５の先端は飛灰無害化槽４内に開口している。な
お、２３は種晶戻し配管１５に設けられた弁である。That is, in this embodiment, as shown in FIGS. 1 and 2, the seed crystal returning pipe 15 is branched from the portion of the dewatered sludge supply pipe 21 upstream of the valve 22. Is open at the inside of the fly ash detoxification tank 4. Reference numeral 23 is a valve provided in the seed crystal returning pipe 15.
【００１７】本実施例では、飛灰汚泥濃縮槽６より飛灰
汚泥移送ポンプ７によって脱水機汚泥供給配管２１内に
導入された濃縮された炭酸カルシウムのスラリーは、種
晶戻し配管１５を経て種晶として飛灰無害化槽４へ再循
環される。これによって、飛灰無害化槽４内においてス
ケールの種晶となる炭酸カルシウムの液中濃度が高めら
れて犠牲面としての炭酸カルシウムの表面積が増大し、
吹き出しノズル１３の先端部１４近傍における炭酸カル
シウムの飽和濃度を下げてスケールの析出を緩和するこ
とができ、その結果、吹き出しノズル１３の先端部１４
に炭酸カルシウムがスケールとして付着することが防止
され、吹き出しノズル１３の閉塞を防ぐことができる。In this embodiment, the concentrated calcium carbonate slurry introduced into the dehydrator sludge supply pipe 21 from the fly ash sludge concentrating tank 6 by the fly ash sludge transfer pump 7 is passed through the seed crystal returning pipe 15 and seeded. The crystals are recycled to the fly ash detoxification tank 4. As a result, the concentration of calcium carbonate in the fly ash detoxification tank 4 as seed crystals of scale is increased, and the surface area of calcium carbonate as a sacrificial surface is increased.
The saturation concentration of calcium carbonate in the vicinity of the tip 14 of the blowing nozzle 13 can be reduced to mitigate scale deposition, and as a result, the tip 14 of the blowing nozzle 13 can be reduced.
It is possible to prevent calcium carbonate from adhering to the above as a scale, and to prevent the blowing nozzle 13 from being blocked.
【００１８】前記本発明の一実施例及び比較例として従
来の方法を用いた試験結果を示す。Test results using a conventional method will be shown as an example of the present invention and a comparative example.
【００１９】（比較例（従来方法））図３及び図４に示
す従来方法で、飛灰無害化槽４（６ｍ3 ）に排ガスを流
量３０Ｎｍ3 ／ｍｉｎ（ＣＯ2 濃度１２ｖｏｌ％）で供
給した。飛灰無害化槽４内のスラリー濃度は３ｗｔ％と
し、そのうち炭酸カルシウムスラリー濃度を１．５ｗｔ
％とした。この条件で１カ月間連続運転を実施したとこ
ろ、排ガス吹き出しノズル１３（６５φｍｍ）の先端部
１４の外側に厚さ約１０ｍｍ、内側に厚さ約２５ｍｍの
スケールが付着し、排ガス供給ファン１１の吐出圧が上
昇するとともに排ガス流量が減少し、ＣＯ2 による中和
能力が低下した。吹き出しノズル１３の先端部１４の炭
酸カルシウムの過飽和度を測定した結果１．４（溶解炭
酸カルシウム／飽和炭酸カルシウム）と非常に高い値で
あった。この結果を、図５のグラフにおいて、△で示
す。(Comparative Example (Conventional Method)) Exhaust gas was supplied to the fly ash detoxification tank 4 (6 m 3 ) at a flow rate of 30 Nm 3 / min (CO 2 concentration 12 vol%) by the conventional method shown in FIGS. 3 and 4. . The slurry concentration in the fly ash detoxification tank 4 is set to 3 wt%, of which the calcium carbonate slurry concentration is 1.5 wt.
%. When continuous operation was carried out for one month under these conditions, a scale with a thickness of about 10 mm and a thickness of about 25 mm adhered to the outside of the tip portion 14 of the exhaust gas discharge nozzle 13 (65 φmm), and the discharge of the exhaust gas supply fan 11 The exhaust gas flow rate decreased as the pressure increased, and the neutralization ability by CO 2 decreased. As a result of measuring the degree of supersaturation of calcium carbonate in the tip portion 14 of the blowing nozzle 13, it was a very high value of 1.4 (dissolved calcium carbonate / saturated calcium carbonate). This result is indicated by Δ in the graph of FIG.
【００２０】（実施例（本発明））図１及び図２に示さ
れる本発明の実施例において、飛灰無害化槽４（６
ｍ3 ）に種晶として流量５ｍ3 ／ｈｒで飛灰汚泥濃縮槽
６のスラリーを供給した。排ガス５は流量３０Ｎｍ3 ／
ｍｉｎ（ＣＯ2 濃度１２ｖｏｌ％）で飛灰無害化槽４に
供給した。飛灰無害化槽４内のスラリー濃度は１０ｗｔ
％で、そのうち炭酸カルシウムスラリー濃度は種晶分を
含み５ｗｔ％とした。１カ月間連続運転を実施したとこ
ろ、排ガス吹き出しノズル１３（６５φｍｍ）の先端部
１４の外側及び内側にもスケールは全く付着しなかっ
た。また、吹き出しノズル１３のノズル先端部１４の炭
酸カルシウムの過飽和度を測定した結果、１．１と低い
値であった。この結果を、図５のグラフで○で示す。(Example (Invention)) In the embodiment of the present invention shown in FIGS. 1 and 2, the fly ash detoxification tank 4 (6)
m 3 ), the slurry of the fly ash sludge concentrating tank 6 was supplied as a seed crystal at a flow rate of 5 m 3 / hr. Exhaust gas 5 has a flow rate of 30 Nm 3 /
It was supplied to the fly ash detoxification tank 4 with min (CO 2 concentration 12 vol%). The slurry concentration in the fly ash detoxification tank 4 is 10 wt.
%, Of which the calcium carbonate slurry concentration was 5 wt% including seed crystals. When the continuous operation was carried out for one month, no scale adhered to the outside and the inside of the tip portion 14 of the exhaust gas blowing nozzle 13 (65 mm). Further, the result of measuring the degree of supersaturation of calcium carbonate in the nozzle tip portion 14 of the blowing nozzle 13 was 1.1, which was a low value. This result is shown by a circle in the graph of FIG.
【００２１】また、図１及び図２に示される本発明の実
施例において、飛灰汚泥濃縮槽６のスラリーの飛灰無害
化槽４への供給流量を変化させ、飛灰無害化槽４内の炭
酸カルシウムスラリー濃度を変えた。その時の吹き出し
ノズル１３の先端部１４の炭酸カルシウムの過飽和度、
ノズル先端の外側へのスケール付着量と炭酸カルシウム
スラリー濃度の関係が図５に示されている。In the embodiment of the present invention shown in FIGS. 1 and 2, the flow rate of the slurry in the fly ash sludge concentrating tank 6 supplied to the fly ash detoxification tank 4 is changed so that the inside of the fly ash detoxification tank 4 is changed. The calcium carbonate slurry concentration was changed. The degree of supersaturation of calcium carbonate at the tip portion 14 of the blowing nozzle 13 at that time,
The relationship between the amount of scale adhered to the outside of the nozzle tip and the calcium carbonate slurry concentration is shown in FIG.
【００２２】以上の試験結果から、本発明の前記実施例
は、吹き出しノズルの先端部へのスケールの付着を防止
することができることが判明し、特に、炭酸カルシウム
スラリー濃度を３ｗｔ％以上（炭酸カルシウム過飽和度
で１．１５以下）にすることによって月間の吹き出しノ
ズル１３の先端部１４の外側の炭酸カルシウムのスケー
ルの付着量を１ｍｍ以下とすることができ、２〜３ケ月
に１度メンテナンスのために吹き出しノズル１３を引き
上げてスケールを取り除くことによって、飛灰無害化槽
の中和能力を低下することなく連続運転を行うことがで
きることが判明した。From the above test results, it was found that the above-mentioned embodiment of the present invention can prevent the scale from adhering to the tip portion of the blowing nozzle, and in particular, the calcium carbonate slurry concentration is 3 wt% or more (calcium carbonate). By setting the degree of supersaturation to 1.15 or less), it is possible to reduce the amount of calcium carbonate scale adhered on the outer side of the tip portion 14 of the blowing nozzle 13 per month to 1 mm or less, and once every 2-3 months for maintenance. It was found that continuous operation can be performed without lowering the neutralization capacity of the fly ash detoxification tank by pulling up the blowing nozzle 13 and removing the scale.
【００２３】[0023]
【発明の効果】本発明は、水で溶解された飛灰を収容し
た飛灰無害化槽に炭酸ガスを含む排ガスを吹き出しノズ
ルより吹き込んで飛灰中に含まれる未反応アルカリ分を
中和する際に生成された炭酸カルシウムを、濃縮した上
種晶として飛灰無害化槽へ再循環させているために、前
記排ガスの吹き出しノズルにおける炭酸カルシウムのス
ケールを確実に防止することができ、吹き出しノズルの
閉塞を防いで飛灰無害化槽における中和能力を低下させ
ることなく連続した飛灰の中和処理を行うことができ
る。INDUSTRIAL APPLICABILITY According to the present invention, an exhaust gas containing carbon dioxide gas is blown from a blowing nozzle into a fly ash detoxification tank containing fly ash dissolved in water to neutralize unreacted alkaline components contained in the fly ash. Since the calcium carbonate generated at this time is recirculated to the fly ash detoxification tank as a concentrated upper seed crystal, the scale of calcium carbonate in the exhaust gas blowing nozzle can be reliably prevented, and the blowing nozzle It is possible to carry out continuous neutralization treatment of fly ash without blocking the clogging of the ash and without lowering the neutralization ability in the fly ash detoxification tank.
【図１】本発明の一実施例のフロー図である。FIG. 1 is a flow chart of an embodiment of the present invention.
【図２】同実施例の飛灰無害化槽の断面図である。FIG. 2 is a sectional view of a fly ash detoxification tank of the same example.
【図３】従来の飛灰の排ガス中和処理方法のフロー図で
ある。FIG. 3 is a flow chart of a conventional method for neutralizing exhaust gas of fly ash.
【図４】図３に示される従来の方法の飛灰無害化槽の断
面図である。FIG. 4 is a sectional view of the fly ash detoxification tank of the conventional method shown in FIG.
【図５】炭酸カルシウム過飽和度、スケール付着量と炭
酸カルシウムスラリー濃度の関係を示すグラフである。FIG. 5 is a graph showing the relationship between the degree of calcium carbonate supersaturation, the amount of scale adhesion, and the concentration of calcium carbonate slurry.
１ 飛灰 ２ 飛灰溶解槽 ２ａ 攪拌機 ３ 灰汚水槽 ４ 飛灰無害化槽 ４ａ 攪拌機 ５ 排ガス ６ 飛灰汚泥濃縮槽 ７ 飛灰汚泥移送ポンプ ８ 脱水機 ９ 脱水汚泥 １０ 飛灰ホッパ １１ 排ガス供給ファン １２ 炉内 １３ 吹き出しノズル １４ 吹き出しノズルの先端部 １５ 種晶戻し配管 １６ 配管 １７ 出口ノズル １８ 灰沈でん槽 １９ トラック ２０ 灰汚水処理装置 ２１ 脱水機汚泥供給配管 ２２，２３ 弁 1 Fly ash 2 Fly ash dissolution tank 2a Stirrer 3 Ash sewage tank 4 Fly ash detoxification tank 4a Stirrer 5 Exhaust gas 6 Fly ash sludge concentrating tank 7 Fly ash sludge transfer pump 8 Dehydrator 9 Dewatered sludge 10 Fly ash hopper 11 Exhaust gas supply fan 12 Inside of furnace 13 Blow-out nozzle 14 Tip of blow-out nozzle 15 Seed crystal return pipe 16 Pipe 17 Exit nozzle 18 Ash settling tank 19 Truck 20 Ash sewage treatment device 21 Dehydrator sludge supply pipe 22, 23 Valve
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｂ０９Ｂ 3/00 ３０４ Ｇ ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification code Office reference number FI technical display location B09B 3/00 304 G
Claims (1)
槽に炭酸ガスを含む排ガスを吹き出しノズルより吹き込
んで飛灰中に含まれる未反応アルカリ分を中和する飛灰
の排ガス中和処理方法において、前記中和によって生成
された炭酸カルシウムを濃縮した上種晶として前記飛灰
無害化槽へ再循環させて、前記排ガスの吹き出しノズル
への炭酸カルシウムのスケールの付着を防止することを
特徴とする飛灰の排ガス中和処理方法。1. In the fly ash exhaust gas, in which the fly ash detoxification tank containing water in which the fly ash is dissolved is blown with an exhaust gas containing carbon dioxide gas from a blowing nozzle to neutralize unreacted alkali components contained in the fly ash. In the Japanese treatment method, calcium carbonate produced by the neutralization is recirculated to the fly ash detoxification tank as a concentrated upper seed crystal to prevent calcium carbonate scale from adhering to the exhaust gas blowing nozzle. A method for neutralizing exhaust gas from fly ash, which is characterized by:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24761794A JPH08108038A (en) | 1994-10-13 | 1994-10-13 | Fly ash waste gas neutralization treating method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24761794A JPH08108038A (en) | 1994-10-13 | 1994-10-13 | Fly ash waste gas neutralization treating method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH08108038A true JPH08108038A (en) | 1996-04-30 |
Family
ID=17166179
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP24761794A Withdrawn JPH08108038A (en) | 1994-10-13 | 1994-10-13 | Fly ash waste gas neutralization treating method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH08108038A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2004030839A1 (en) * | 2002-10-07 | 2004-04-15 | Taiheiyo Cement Corporation | Method and apparatus for treating calcium-containing powder |
| WO2007023937A1 (en) | 2005-08-26 | 2007-03-01 | Taiheiyo Cement Corporation | Apparatus and method for dissolution/reaction |
| US7837963B2 (en) | 2006-10-24 | 2010-11-23 | Taiheiyo Cement Corporation | Method for removing lead from cement burning furnace |
| US8282263B2 (en) | 2005-10-31 | 2012-10-09 | Taiheiyo Cement Corporation | Apparatus and method for adding wet ash to cement |
| US8439202B2 (en) | 2006-12-05 | 2013-05-14 | Taiheiyo Cement Corporation | Coal ash treatment method and apparatus |
| US8893892B2 (en) | 2005-12-07 | 2014-11-25 | Taiheiyo Cement Corporation | Apparatus and method for removing unburned carbon from fly ash |
| JP2015096810A (en) * | 2013-11-15 | 2015-05-21 | 株式会社東芝 | Contaminated fly ash treatment method and contaminated fly ash treatment system |
| CN113332927A (en) * | 2021-05-25 | 2021-09-03 | 杭州灰弘环保科技有限公司 | Novel coupling system and method for pulping, washing and carbon neutralization of waste incineration fly ash |
-
1994
- 1994-10-13 JP JP24761794A patent/JPH08108038A/en not_active Withdrawn
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2004030839A1 (en) * | 2002-10-07 | 2004-04-15 | Taiheiyo Cement Corporation | Method and apparatus for treating calcium-containing powder |
| WO2007023937A1 (en) | 2005-08-26 | 2007-03-01 | Taiheiyo Cement Corporation | Apparatus and method for dissolution/reaction |
| US7947229B2 (en) | 2005-08-26 | 2011-05-24 | Taiheiyo Cement Corporation | Apparatus and method for dissolution reaction |
| JP5436777B2 (en) * | 2005-08-26 | 2014-03-05 | 太平洋セメント株式会社 | Dissolution reactor |
| KR101429649B1 (en) * | 2005-08-26 | 2014-08-13 | 다이헤이요 세멘토 가부시키가이샤 | Apparatus and method for dissolution／reaction |
| US8282263B2 (en) | 2005-10-31 | 2012-10-09 | Taiheiyo Cement Corporation | Apparatus and method for adding wet ash to cement |
| US8893892B2 (en) | 2005-12-07 | 2014-11-25 | Taiheiyo Cement Corporation | Apparatus and method for removing unburned carbon from fly ash |
| US7837963B2 (en) | 2006-10-24 | 2010-11-23 | Taiheiyo Cement Corporation | Method for removing lead from cement burning furnace |
| US8439202B2 (en) | 2006-12-05 | 2013-05-14 | Taiheiyo Cement Corporation | Coal ash treatment method and apparatus |
| JP2015096810A (en) * | 2013-11-15 | 2015-05-21 | 株式会社東芝 | Contaminated fly ash treatment method and contaminated fly ash treatment system |
| CN113332927A (en) * | 2021-05-25 | 2021-09-03 | 杭州灰弘环保科技有限公司 | Novel coupling system and method for pulping, washing and carbon neutralization of waste incineration fly ash |
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