JP3513120B2 - Treatment of water containing dioxins - Google Patents
Treatment of water containing dioxinsInfo
- Publication number
- JP3513120B2 JP3513120B2 JP2001188242A JP2001188242A JP3513120B2 JP 3513120 B2 JP3513120 B2 JP 3513120B2 JP 2001188242 A JP2001188242 A JP 2001188242A JP 2001188242 A JP2001188242 A JP 2001188242A JP 3513120 B2 JP3513120 B2 JP 3513120B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- dioxins
- reverse osmosis
- treating
- osmosis membrane
- 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 - Fee Related
Links
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Treatment Of Sludge (AREA)
- Cleaning By Liquid Or Steam (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、ダイオキシン類を
高濃度で含有する水を処理する方法に関する。TECHNICAL FIELD The present invention relates to a method for treating water containing dioxins at a high concentration.
【０００２】[0002]
【従来の技術および発明が解決しようとする課題】従
来、ゴミ焼却場や、工場から排出される各種産業廃棄物
の焼却炉から排出される多量の灰の埋立地（処分場）か
ら流出する浸出水には、多くの塩分や有機物が含まれて
おり、そのまま河川等に放流することはできないため、
環境汚染を防止するために、種々の方法が提案されてい
る。[Background Art] [Problems to be Solved by the Invention] Conventionally, a large amount of ash discharged from a refuse incinerator or an incinerator of various industrial waste discharged from a factory is leached from a landfill (disposal site). Water contains a lot of salt and organic matter and cannot be discharged to rivers as it is.
Various methods have been proposed to prevent environmental pollution.
【０００３】例えば、図２に示すように、処分場３１か
らの浸出水は流量調整設備３２にて流量を調整された
後、カルシウム除去設備３３に供給され、炭酸ソーダ、
ポリマー、凝集剤およびアルカリなどが浸出水に添加さ
れてカルシウムが除去され、さらに、その水は生物処理
設備３４において、微生物により有機物が分解され、凝
集・沈殿設備３５において、ポリマー、凝集剤、酸、ア
ルカリなどが添加されて凝集・沈殿化が図られ、さら
に、ｐＨ調整のために必要に応じて酸、アルカリなどが
被処理水に添加され、砂濾過設備３６で濾過された後、
活性炭吸着設備３７において、有機物は活性炭に吸着・
除去され、キレート吸着処理３８を経て濃縮設備３９で
濃縮水と透過水に分離され、透過水は経路４０を経て河
川等に放流されていた。For example, as shown in FIG. 2, after the flow rate of the leachate from the disposal site 31 is adjusted by the flow rate adjusting facility 32, the leachate is supplied to the calcium removing facility 33, soda carbonate,
A polymer, a coagulant, an alkali, etc. are added to the leachate to remove calcium, and further, in the water, the organic matter is decomposed by the microorganisms in the biological treatment facility 34, and the polymer, the coagulant, the acid in the flocculation / precipitation facility 35. , Alkali, etc. are added to achieve aggregation / precipitation, and further, acid, alkali, etc. are added to the water to be treated as necessary for pH adjustment, and after being filtered by the sand filtration facility 36,
In the activated carbon adsorption equipment 37, organic substances are adsorbed on the activated carbon.
After being removed, it was separated into concentrated water and permeated water in the concentrating facility 39 through the chelate adsorption treatment 38, and the permeated water was discharged to a river or the like via the route 40.
【０００４】ところで、焼却炉の焼却灰中にダイオキシ
ン、ジベンゾフランおよびコプラナＰＣＢからなるダイ
オキシン類が含まれている場合、処分場からの浸出水に
ダイオキシン類が含まれるので、このダイオキシン類が
自然環境を破壊しないように、浸出水を何らかの方法で
処理し、ダイオキシン類を除去する必要がある。しか
し、ダイオキシン類は化学的に安定な物質であるため、
図２に示すような、生物処理と活性炭吸着処理を組み合
わせるだけでは、その完全な除去は困難である。特に、
廃棄物焼却炉の解体部品を洗浄した洗浄水のように、高
濃度のダイオキシン類を含む水を処理する場合には、特
別の処理技術が必要である。By the way, when dioxins composed of dioxins, dibenzofuran and coplana PCB are contained in the incineration ash of the incinerator, since dioxins are contained in the leachate from the disposal site, these dioxins can improve the natural environment. The leachate must be treated in some way to remove dioxins to prevent destruction. However, because dioxins are chemically stable substances,
Complete removal is difficult only by combining biological treatment and activated carbon adsorption treatment as shown in FIG. In particular,
When treating water containing high concentration of dioxins such as washing water used for washing dismantled parts of a waste incinerator, a special treatment technique is required.
【０００５】例えば、ダイオキシン類を高濃度で含有す
る水を直接促進酸化するか、または凝集沈殿処理、生物
処理、砂濾過等の前処理を行った後、促進酸化する方法
が提案されている。直接促進酸化とは、ダイオキシン類
を含有する水に紫外線またはオゾンを照射してダイオキ
シン類を分解処理する方法である。しかし、この方法
は、水中の懸濁物質等の不純物によって紫外線またはオ
ゾンが遮られるのでダイオキシン類の分解率が７０〜８
０％と低く、ダイオキシン類を高濃度で含有する水の処
理方法としては好ましくない。また、凝集沈殿処理等の
前処理を行った後に促進酸化する方法を採用する場合、
かなりの量のダイオキシン類が凝集沈殿汚泥等の前処理
汚泥に移行するが、このダイオキシン類含有汚泥を処理
する技術が確立されていなかったので、結果として、凝
集沈殿汚泥中のダイオキシン類は十分な処理ができなか
った。For example, there has been proposed a method in which water containing dioxins at a high concentration is directly promoted to be oxidized, or a pretreatment such as coagulation-sedimentation treatment, biological treatment and sand filtration is carried out, followed by accelerated oxidation. The direct accelerated oxidation is a method of decomposing dioxins by irradiating water containing dioxins with ultraviolet rays or ozone. However, in this method, ultraviolet rays or ozone are blocked by impurities such as suspended substances in water, so that the decomposition rate of dioxins is 70 to 8%.
It is as low as 0%, which is not preferable as a method for treating water containing a high concentration of dioxins. Further, when adopting a method of promoting oxidation after performing a pretreatment such as coagulation sedimentation treatment,
A considerable amount of dioxins is transferred to the pretreatment sludge such as coagulation sedimentation sludge, but the technology for treating this dioxins-containing sludge has not been established. It could not be processed.
【０００６】本発明は従来の技術の有する上記問題点に
鑑みてなされたものであり、その目的は、ダイオキシン
類を高濃度で含有する水を処理した処理水及び汚泥中の
ダイオキシン類をほぼ完全に分解しうる方法を提供する
ことにある。The present invention has been made in view of the above problems of the prior art, and an object thereof is to treat treated water obtained by treating water containing a high concentration of dioxins and dioxins in sludge. Provide a method that can be decomposed into
Especially .
【０００７】[0007]
【課題を解決するための手段】上記目的を達成するため
に本発明によれば、ダイオキシン類を高濃度で含有する
汚泥と乾燥物を以下の方法により処理することととして
いる。To achieve the above object, according to the present invention, a sludge containing a high concentration of dioxins and a dried product are treated by the following method.
There is .
【０００８】[0008]
【０００９】[0009]
【発明の実施の形態】すなわち、本願は、ダイオキシン
類を含有する水の処理方法であって、該ダイオキシン類
含有水を凝集沈澱槽で処理液と汚泥に分離し、上記処理
液を膜分離装置で処理水と濃縮水に分離し、該濃縮水を
蒸発乾燥装置で乾燥物と凝縮水に分離し、上記汚泥と該
乾燥物を酸化雰囲気下で５５０〜７５０℃で焼成し、さ
らに、不活性ガス雰囲気または酸素濃度が３％以下であ
る酸素欠乏雰囲気下で３００〜５５０℃に加熱し、次い
で、冷却することを特徴とするダイオキシン類含有水の
処理方法を提供する。この本願発明によれば、酸化雰囲
気下で５５０〜７５０℃の焼成により、微生物による分
解が困難な有機物を酸化分解し、酸素欠乏状態の特定雰
囲気で３００〜５５０℃に加熱することによりダイオキ
シン類を分解し、その後、冷却することによりダイオキ
シン類が再生されることはない。BEST MODE FOR CARRYING OUT THE INVENTION That is, the present application relates to dioxin.
A method for treating water containing compounds, wherein the dioxin-containing water is separated into a treatment liquid and sludge in a coagulation sedimentation tank, and the treatment liquid is separated into treated water and concentrated water by a membrane separator, Is separated into a dried product and condensed water by an evaporative drying device, and the sludge and the dried product are calcined at 550 to 750 ° C. in an oxidizing atmosphere.
In addition, an inert gas atmosphere or oxygen concentration of 3% or less
In an oxygen-deficient atmosphere, heat to 300-550 ° C and then
Water containing dioxin characterized by cooling
Provide a processing method. According to the present invention, the oxidizing atmosphere
By calcination at 550 to 750 ° C under air,
Oxygen-decomposing organic matter that is difficult to solve,
By heating to 300-550 ° C in ambient air
Dioxins are not regenerated by decomposing syn and then cooling.
【００１０】[0010]
【００１１】[0011]
【００１２】以上のような処理方法を実施するための装
置としては、ダイオキシン類含有水を処理液と汚泥に分
離する凝集沈殿槽と、上記処理液を処理水と濃縮水に分
離する膜分離装置と、上記濃縮水を乾燥物と凝縮水に分
離する蒸発乾燥装置と、上記汚泥と乾燥物を焼成する焼
成炉と、焼成後の汚泥と乾燥物を冷却する冷却容器とを
備え、凝集沈殿槽から、膜分離装置、蒸発乾燥装置およ
び焼成炉を経て冷却容器に至る経路によりこれらの装置
を接続したものが好ましい。As an apparatus for carrying out the above treatment method, a coagulating sedimentation tank for separating dioxin-containing water into treatment liquid and sludge, and a membrane separation device for separating the treatment liquid into treatment water and concentrated water An evaporative drying device that separates the concentrated water into dry matter and condensed water, a firing furnace that fires the sludge and the dried matter, and a cooling container that cools the sludge and the dried matter after firing, and a coagulation sedimentation tank It is preferable that these devices are connected by a path from the membrane separator, the evaporative dryer, and the firing furnace to the cooling container.
【００１３】また、蒸発乾燥装置で得た凝縮水を凝集沈
殿槽に返送すれば、凝縮水は循環処理されて、全て膜分
離処理水となるという効果がある。Further, if the condensed water obtained by the evaporative drying apparatus is returned to the coagulation sedimentation tank, the condensed water is circulated and all becomes membrane separation treated water.
【００１４】さらに、膜分離装置が逆浸透膜であれば、
ダイオキシン類の除去と共に塩類、その他有機物等の汚
染物を除去することができるという効果がある。Further, if the membrane separation device is a reverse osmosis membrane,
There is an effect that salts and other contaminants such as organic substances can be removed together with the removal of dioxins.
【００１５】そして、逆浸透膜を複数段で構成し、後段
側の逆浸透膜で分離した濃縮水を前段側の逆浸透膜に返
送すれば、逆浸透膜で分離後の処理水質が向上するとい
う効果がある。If the reverse osmosis membrane is composed of a plurality of stages and the concentrated water separated by the reverse osmosis membrane on the rear side is returned to the reverse osmosis membrane on the front side, the quality of treated water after separation by the reverse osmosis membrane is improved. There is an effect.
【００１６】また、ダイオキシン類を含有する水が、焼
却炉または焼却炉解体部材を洗浄した後の洗浄排水であ
って、膜分離装置で得られる処理水を焼却炉または焼却
炉解体部材を洗浄する洗浄水として再利用すれば、処理
水をクローズドシステムで循環使用し、処理水を外部へ
放出することはないので、環境を汚染することはない。Further, the water containing dioxins is the cleaning waste water after cleaning the incinerator or the incinerator dismantling member, and the treated water obtained in the membrane separator is used to clean the incinerator or the incinerator dismantling member. If reused as wash water, the treated water is circulated in a closed system and the treated water is not discharged to the outside, so that it does not pollute the environment.
【００１７】[0017]
【実施例】以下に本発明の実施例を図面を参照しながら
説明する。Embodiments of the present invention will be described below with reference to the drawings.
【００１８】図１は、本発明の処理方法を実施するに好
適である装置の概略構成図である。図１において、１は
各種産業廃棄物の焼却炉を解体した部品を示し、２は洗
浄器具、３は洗浄後の水を受ける貯槽である。４は凝集
沈殿槽であり、凝集沈殿槽４の上澄液は貯槽５を経て一
段目逆浸透膜６に送られる。一段目逆浸透膜６を透過し
た透過水は二段目逆浸透膜７に送られる。二段目逆浸透
膜７を透過した透過水は貯槽８、経路２７を経て洗浄器
具２の洗浄水として利用される。FIG. 1 is a schematic configuration diagram of an apparatus suitable for carrying out the processing method of the present invention. In FIG. 1, 1 is a disassembled part of an incinerator for various industrial wastes, 2 is a cleaning instrument, and 3 is a storage tank for receiving water after cleaning. 4 is a coagulation sedimentation tank, and the supernatant of the coagulation sedimentation tank 4 is sent to a first-stage reverse osmosis membrane 6 via a storage tank 5. The permeated water that has passed through the first-stage reverse osmosis membrane 6 is sent to the second-stage reverse osmosis membrane 7. The permeated water that has permeated through the second-stage reverse osmosis membrane 7 is used as cleaning water for the cleaning device 2 via the storage tank 8 and the path 27.
【００１９】一段目逆浸透膜６で濃縮された濃縮水は、
高温蒸気を熱源とする蒸発乾燥装置９で乾燥物と凝縮水
に分離される。この乾燥物と上記凝集沈殿槽４で分離さ
れた汚泥は、貯槽１０を経て焼成炉１１に供給される。
汚泥と乾燥物は焼成炉１１において、別々に焼成するこ
ともできるし、汚泥と乾燥物を同時に焼成することもで
きる。１２は電気ヒータであり、電気ヒータ１２に通電
することにより、焼成炉１１を加熱する。The concentrated water concentrated by the first-stage reverse osmosis membrane 6 is
It is separated into dry matter and condensed water by an evaporative drying device 9 using high temperature steam as a heat source. The dried product and the sludge separated in the coagulating sedimentation tank 4 are supplied to the firing furnace 11 via the storage tank 10.
The sludge and the dried product can be fired separately in the firing furnace 11, or the sludge and the dried substance can be fired at the same time. An electric heater 12 heats the firing furnace 11 by energizing the electric heater 12.
【００２０】１３は焼成炉１１に空気を供給するための
コンプレッサー、１４は窒素ボンベである。１５は冷却
容器であり、ジャケット１６に通水することにより冷却
容器１５は急冷される。１７は、回収された焼成固形物
を運搬するトラックである。Reference numeral 13 is a compressor for supplying air to the firing furnace 11, and 14 is a nitrogen cylinder. Reference numeral 15 denotes a cooling container, and the cooling container 15 is rapidly cooled by passing water through the jacket 16. Reference numeral 17 is a truck for carrying the recovered calcined solid matter.
【００２１】以上のように構成されるシステムにより、
廃棄物焼却炉解体部品の洗浄水を処理する方法について
説明する。With the system configured as described above,
A method for treating the cleaning water for the waste incinerator dismantling parts will be described.
【００２２】焼却炉解体部品１を洗浄した後の高濃度の
ダイオキシン類を含有する水は貯槽３を経て凝集沈殿槽
４に送られて、汚泥と上澄液に分離される。そして、汚
泥は経路１８を経て貯槽１０に送られる。一方、上澄液
は貯槽５を経て一段目逆浸透膜６に送られ、濃縮水と透
過水に分離される。この濃縮水は経路１９を経て蒸発乾
燥装置９に送られ、ジャケット２０に通入した高温蒸気
により約１００〜１５０℃に加熱されて、乾燥物と凝縮
水を得る。この凝縮水を経路２１を経て貯槽３に戻すこ
とにより、すべての水が膜分離処理され、高清浄度の処
理水質となって再利用されるという効果がある。The water containing the high concentration of dioxins after cleaning the incinerator dismantling part 1 is sent to the coagulating sedimentation tank 4 via the storage tank 3 and separated into sludge and supernatant liquid. Then, the sludge is sent to the storage tank 10 via the path 18. On the other hand, the supernatant liquid is sent to the first-stage reverse osmosis membrane 6 through the storage tank 5 and separated into concentrated water and permeated water. This concentrated water is sent to the evaporative drying device 9 via the path 19 and heated to about 100 to 150 ° C. by the high temperature steam passing through the jacket 20 to obtain a dried product and condensed water. By returning the condensed water to the storage tank 3 via the path 21, all the water is subjected to the membrane separation treatment, and has the effect of being reused as the treated water quality of high cleanliness.
【００２３】一段目逆浸透膜６を透過した透過水は二段
目逆浸透膜７に送られ、濃縮水と透過水に分離される。
この透過水は貯槽８を経て洗浄器具２の洗浄水として利
用される。２段目逆浸透膜７で濃縮された濃縮水は経路
２２を経て一段目逆浸透膜６の入側に送られ、再び、一
段目逆浸透膜６において濃縮水と透過水に分離される。
このように、逆浸透膜を複数段で構成し、後段側の逆浸
透膜で分離した濃縮水を前段側の逆浸透膜に供給すれ
ば、処理水質を向上しうるという効果があるので好まし
い。The permeated water that has permeated through the first-stage reverse osmosis membrane 6 is sent to the second-stage reverse osmosis membrane 7 and separated into concentrated water and permeated water.
This permeated water passes through the storage tank 8 and is used as cleaning water for the cleaning implement 2. The concentrated water concentrated in the second-stage reverse osmosis membrane 7 is sent to the inlet side of the first-stage reverse osmosis membrane 6 via the path 22, and is again separated into the concentrated water and the permeated water in the first-stage reverse osmosis membrane 6.
As described above, it is preferable that the reverse osmosis membrane is composed of a plurality of stages and the concentrated water separated by the reverse osmosis membrane on the rear side is supplied to the reverse osmosis membrane on the front side, because the treated water quality can be improved.
【００２４】かくして、凝集沈殿槽４で分離された汚泥
と蒸発乾燥装置９で得た乾燥物は貯槽１０を経て、同時
にあるいは別々に焼成炉１１に送られる。そして、コン
プレッサー１３から経路２３を経て焼成炉１１内に空気
を送り、同時に電気ヒータ１２により焼成炉１１内を３
００〜７５０℃に加熱し、炉内の乾燥物と汚泥を焼成
し、有機物を燃焼させて除去する。約２〜５時間後にコ
ンプレッサー１３の運転を止め、窒素ボンベ１４から経
路２４を経て焼成炉１１内に窒素を供給し、炉内の雰囲
気を完全に窒素に置換する。このように炉内を酸素欠乏
状態にして電気ヒーター１２により焼成炉１１内の温度
を３００〜５５０℃に加熱し、炉内に存在するダイオキ
シンを酸素欠乏状態で分解する。２５はポンプ、２６は
バルブである。Thus, the sludge separated in the coagulating sedimentation tank 4 and the dried product obtained in the evaporative drying device 9 are sent to the firing furnace 11 through the storage tank 10 simultaneously or separately. Then, air is sent from the compressor 13 to the inside of the firing furnace 11 via the path 23, and at the same time, the electric heater 12 moves the inside of the firing furnace 11 to 3
It is heated to 00 to 750 ° C., the dried material and sludge in the furnace are burned, and the organic matter is burned and removed. After about 2 to 5 hours, the operation of the compressor 13 is stopped, nitrogen is supplied into the firing furnace 11 from the nitrogen cylinder 14 via the path 24, and the atmosphere in the furnace is completely replaced with nitrogen. In this way, the temperature in the firing furnace 11 is heated to 300 to 550 ° C. by the electric heater 12 in the oxygen-deficient state, and the dioxin existing in the furnace is decomposed in the oxygen-deficient state. 25 is a pump and 26 is a valve.
【００２５】約１時間後に窒素ボンベ１４からの窒素の
供給と電気ヒーター１２の通電を停止し、焼成炉１１内
に存在する塩（ＮａＣｌ等）を冷却容器１５に移してジ
ャケット１６に水を通入して冷却容器内の塩を４０〜６
０℃まで急冷する。以上のような工程を経て、高品位の
塩を回収することができる。After about 1 hour, the supply of nitrogen from the nitrogen cylinder 14 and the energization of the electric heater 12 are stopped, the salt (NaCl or the like) present in the firing furnace 11 is transferred to the cooling container 15, and water is passed through the jacket 16. Put the salt in the cooling container to 40 ~ 6
Quench to 0 ° C. High-quality salt can be recovered through the above-described steps.
【００２６】以上の実施例は、主として第三の発明に従
った方法であるが、第一の発明のように、汚泥と乾燥物
を不活性ガス雰囲気または酸素濃度が３％以下である酸
素欠乏雰囲気で３００〜５５０℃に加熱し、次いで、急
冷することにより、廃棄物焼却炉解体部品の洗浄水を処
理し、再利用すると共に、汚泥、乾燥物を無害化するこ
ともできるし、第二の発明のように、汚泥と該乾燥物を
酸化雰囲気下で８００℃以上で焼成し、次いで、急冷す
ることにより、廃棄物焼却炉解体部品の洗浄水の処理で
発生する汚泥、乾燥物を無害化することもできる。The above embodiment is mainly the method according to the third invention, but as in the first invention, the sludge and the dried product are treated with an inert gas atmosphere or an oxygen deficiency in which the oxygen concentration is 3% or less. By heating to 300 to 550 ° C. in an atmosphere and then rapidly cooling, the washing water of the waste incinerator dismantling parts can be treated and reused, and the sludge and dried products can be rendered harmless. As in the invention of claim 1, the sludge and the dried product are calcined in an oxidizing atmosphere at 800 ° C. or higher, and then rapidly cooled, so that the sludge and the dried product generated by the treatment of the washing water for the waste incinerator dismantling parts are harmless. It can also be converted.
【００２７】次に、実際に廃棄物焼却炉解体部品を洗浄
した洗浄水を、第三の発明に従った方法により処理した
ので、以下に説明する。Next, the cleaning water for cleaning the waste incinerator dismantling parts was actually treated by the method according to the third aspect of the present invention, which will be described below.
【００２８】すなわち、凝集沈殿槽４の凝集汚泥を処理
する場合は、焼成炉１１を空気雰囲気とし、５５０℃で
１時間焼成し、さらに、炉内を窒素雰囲気に代えて５５
０℃で１時間焼成し、次いで、急冷した。That is, when the coagulated sludge in the coagulation sedimentation tank 4 is treated, the calcining furnace 11 is set to an air atmosphere and calcined at 550 ° C. for 1 hour, and the inside of the furnace is replaced with a nitrogen atmosphere to generate 55.
It was calcined at 0 ° C. for 1 hour and then quenched.
【００２９】また、蒸発乾燥装置９で得た乾燥物を処理
する場合は、焼成炉１１を空気雰囲気とし、６００℃で
１時間焼成し、さらに、炉内を窒素雰囲気に代えて４５
０℃で１時間焼成し、次いで、急冷した。When the dried material obtained by the evaporative drying apparatus 9 is treated, the firing furnace 11 is placed in an air atmosphere and fired at 600 ° C. for 1 hour.
It was calcined at 0 ° C. for 1 hour and then quenched.
【００３０】原洗浄水の性状、二段目逆浸透膜を透過し
た透過水の性状を以下の表１に示し、汚泥と乾燥物の焼
成前後のダイオキシン類濃度について、以下の表２に示
す。The properties of the original wash water and the properties of the permeated water that has permeated the second-stage reverse osmosis membrane are shown in Table 1 below, and the dioxin concentrations before and after firing the sludge and the dried product are shown in Table 2 below.
【００３１】[0031]
【表１】 [Table 1]
【００３２】[0032]
【表２】 [Table 2]
【００３３】表２に示すように、本発明の処理方法によ
れば、高濃度のダイオキシン類を含む洗浄水から、ほぼ
完全にダイオキシン類を分解することができる。また、
表１に示すように、二段目逆浸透膜を透過した透過水の
性状はそのまま河川に放流しても問題のないレベルであ
る。As shown in Table 2, according to the treatment method of the present invention, dioxins can be almost completely decomposed from the wash water containing a high concentration of dioxins. Also,
As shown in Table 1, the property of the permeated water that has permeated through the second-stage reverse osmosis membrane is at a level at which there is no problem even if it is directly discharged into the river.
【００３４】なお、冷却容器１５は設けずに、焼成炉１
１を直接急冷することもできる。例えば、焼成炉１１外
周に冷却水を通入するジャケットを取り付け、このジャ
ケットに冷却水を通入する方法を採用することができ
る。It should be noted that the firing furnace 1 is not provided with the cooling container 15.
It is also possible to directly quench 1. For example, it is possible to adopt a method in which a jacket for passing cooling water is attached to the outer periphery of the firing furnace 11 and cooling water is passed through this jacket.
【００３５】上記実施例では、膜として逆浸透膜を使用
したが、これに限定されるものではなく、限外濾過膜、
精密濾過膜、低圧逆浸透膜等を用いることができる。な
お、逆浸透膜を用いた場合は、より高清浄度な処理水が
得られる点で好ましい。Although the reverse osmosis membrane was used as the membrane in the above-mentioned embodiment, the membrane is not limited to this, and an ultrafiltration membrane,
A microfiltration membrane, a low pressure reverse osmosis membrane, etc. can be used. The use of a reverse osmosis membrane is preferable in that treated water of higher cleanliness can be obtained.
【００３６】[0036]
【発明の効果】本発明は上記のとおり構成されているの
で、以下の効果を奏する。Since the present invention is configured as described above, it has the following effects.
【００３７】請求項１記載の発明によれば、ダイオキシ
ン類を高濃度で含有する水中のダイオキシン類をほぼ完
全に除去することができる。According to the first aspect of the invention, it is possible to almost completely remove dioxins in water containing a high concentration of dioxins.
【００３８】また、請求項２記載の発明によれば、処理
水がすべて膜分離水となり、処理水質が向上するという
効果がある。According to the second aspect of the present invention, all the treated water becomes membrane-separated water, and the quality of the treated water is improved.
【００３９】また、請求項３記載の発明によれば、ダイ
オキシン類、懸濁物質のみならず、他の有機物、塩類も
除去されて処理水質が向上するという効果がある。According to the third aspect of the invention, not only dioxins and suspended substances but also other organic substances and salts are removed, and the quality of treated water is improved.
【００４０】さらに、請求項４記載の発明によれば、処
理水質を一層向上できるという効果がある。Further, according to the invention described in claim 4 , there is an effect that the quality of treated water can be further improved.
【００４１】また、請求項５記載の発明によれば、処理
水をクローズドシステムで循環使用し、処理水を外部へ
放出することはないので、環境を汚染することはない。According to the fifth aspect of the present invention, the treated water is circulated and used in a closed system and the treated water is not discharged to the outside, so that the environment is not polluted.
【００４２】[0042]
【００４３】[0043]
【００４４】[0044]
【００４５】[0045]
【００４６】[0046]
【図１】本発明の処理方法を実施するに好適である装置
の概略構成を示すフロー図である。FIG. 1 is a flow diagram showing a schematic configuration of an apparatus suitable for carrying out a processing method of the present invention.
【図２】従来の排水の処理フローの概略構成を示す図で
ある。FIG. 2 is a diagram showing a schematic configuration of a conventional wastewater treatment flow.
１…廃棄物焼却炉解体部品 ２…洗浄器具 ３、５、８、１０…貯槽 ４…凝集沈殿槽 ６…一段目逆浸透膜 ７…二段目逆浸透膜 ９…蒸発乾燥装置 １１…焼成炉 １２…電気ヒータ １３…コンプレッサー １４…窒素ボンベ １５…冷却容器 １６、２０…ジャケット １７…トラック ２５…ポンプ ２６…バルブ 1 ... Waste incinerator dismantling parts 2 ... Cleaning equipment 3, 5, 8, 10 ... Storage tank 4 ... Coagulation sedimentation tank 6 ... First stage reverse osmosis membrane 7. Second-stage reverse osmosis membrane 9 ... Evaporative drying device 11 ... Baking furnace 12 ... Electric heater 13 ... Compressor 14 ... Nitrogen cylinder 15 ... Cooling container 16, 20 ... Jacket 17 ... Truck 25 ... Pump 26 ... Valve
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ Ｃ０２Ｆ 9/00 Ｃ０２Ｆ 9/00 ５０４Ｅ Ｂ０１Ｄ 61/02 ５００ Ｂ０１Ｄ 61/02 ５００ 61/04 61/04 61/58 61/58 Ｂ０８Ｂ 3/14 Ｂ０８Ｂ 3/14 Ｃ０２Ｆ 1/04 Ｃ０２Ｆ 1/04 Ｚ 1/44 1/44 Ｋ 1/52 1/52 Ｋ 11/10 11/10 Ｚ (72)発明者 小林 俊幸 兵庫県神戸市須磨区南落合１丁目13−９ 275号室 (56)参考文献 特開 平11−188389（ＪＰ，Ａ) 特開2000−279702（ＪＰ，Ａ) 特開2000−230864（ＪＰ，Ａ) 特開2000−61422（ＪＰ，Ａ) 特開2001−79508（ＪＰ，Ａ) 特開2001−79507（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) C02F 9/00 B01D 61/02 B01D 61/04 B01D 61/58 B08B 3/14 C02F 1/04 C02F 1/44 C02F 1/52 C02F 11/10 ─────────────────────────────────────────────────── ─── Continuation of front page (51) Int.Cl. 7 Identification code FI C02F 9/00 C02F 9/00 504E B01D 61/02 500 B01D 61/02 500 61/04 61/04 61/58 61/58 B08B 3/14 B08B 3/14 C02F 1/04 C02F 1/04 Z 1/44 1/44 K 1/52 1/52 K 11/10 11/10 Z (72) Inventor Toshiyuki Kobayashi Suma Ward, Kobe City, Hyogo Prefecture Minami Ochiai 1-Chome 13-9 275 (56) Reference JP-A-11-188389 (JP, A) JP-A-2000-279702 (JP, A) JP-A-2000-230864 (JP, A) JP-A-2000-61422 (JP, A) JP 2001-79508 (JP, A) JP 2001-79507 (JP, A) (58) Fields investigated (Int.Cl. 7 , DB name) C02F 9/00 B01D 61/02 B01D 61/04 B01D 61/58 B08B 3/14 C02F 1/04 C02F 1/44 C02F 1/52 C02F 11/10
Claims (5)
であって、該ダイオキシン類含有水を凝集沈澱槽で処理
液と汚泥に分離し、上記処理液を膜分離装置で処理水と
濃縮水に分離し、該濃縮水を蒸発乾燥装置で乾燥物と凝
縮水に分離し、上記汚泥と該乾燥物を酸化雰囲気下で５
５０〜７５０℃で焼成し、さらに、不活性ガス雰囲気ま
たは酸素濃度が３％以下である酸素欠乏雰囲気下で３０
０〜５５０℃に加熱し、次いで、冷却することを特徴と
するダイオキシン類含有水の処理方法。 1. A method for treating water containing dioxins, comprising separating the dioxins-containing water into a treatment liquid and sludge in a coagulating sedimentation tank, and treating the treatment liquid into treated water and concentrated water with a membrane separator. It separated, the concentrated water is separated in dry matter and condensed water in the evaporative drying apparatus, the sludge and the dried product in an oxidizing atmosphere 5
Calcination at 50 to 750 ° C. , and further 30 in an inert gas atmosphere or an oxygen-deficient atmosphere with an oxygen concentration of 3% or less
A method for treating dioxins-containing water, which comprises heating to 0 to 550 ° C. and then cooling.
記載のダイオキシン類含有水の処理方法。 2. A method according to claim 1 to return the condensed water in the coagulating sedimentation tank
A method for treating water containing dioxins according to the description.
たは２記載のダイオキシン類含有水の処理方法。 3. A film separation apparatus is a reverse osmosis membrane according to claim 1 or
Or the method for treating water containing dioxins according to item 2 .
浸透膜で分離した濃縮水を前段側の逆浸透膜に返送する
請求項３記載のダイオキシン類含有水の処理方法。 4. The reverse osmosis membrane is composed of a plurality of stages, and the concentrated water separated by the reverse osmosis membrane on the rear side is returned to the reverse osmosis membrane on the front side.
The method for treating water containing dioxins according to claim 3 .
または焼却炉解体部材を洗浄した後の洗浄排水であっ
て、膜分離装置で得られる処理水を焼却炉または焼却炉
解体部材を洗浄する洗浄水として再利用することを特徴
とする請求項１、２、３または４記載のダイオキシン類
含有水の処理方法。 5. Water containing dioxins is cleaning waste water after cleaning an incinerator or an incinerator dismantling member, and the treated water obtained by a membrane separator is used to wash the incinerator or incinerator dismantling member. The method for treating dioxins-containing water according to claim 1, 2, 3 or 4, which is reused as washing water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001188242A JP3513120B2 (en) | 2001-06-21 | 2001-06-21 | Treatment of water containing dioxins |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001188242A JP3513120B2 (en) | 2001-06-21 | 2001-06-21 | Treatment of water containing dioxins |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2003001295A JP2003001295A (en) | 2003-01-07 |
| JP3513120B2 true JP3513120B2 (en) | 2004-03-31 |
Family
ID=19027380
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2001188242A Expired - Fee Related JP3513120B2 (en) | 2001-06-21 | 2001-06-21 | Treatment of water containing dioxins |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3513120B2 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010194436A (en) * | 2009-02-24 | 2010-09-09 | Nippon Steel Engineering Co Ltd | Wastewater treatment method |
-
2001
- 2001-06-21 JP JP2001188242A patent/JP3513120B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JP2003001295A (en) | 2003-01-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP3883445B2 (en) | Sewage treatment equipment | |
| JP3009535B2 (en) | Method and apparatus for biologically purifying sewage | |
| WO2007007569A1 (en) | Method for treatment of water containing hardly-degradable substance | |
| JP3394964B2 (en) | Method and apparatus for treating leachate at landfill site | |
| JP5874925B2 (en) | Incineration plant wastewater treatment method and treatment equipment | |
| JP2006192378A (en) | Hardly decomposable substances-containing water treatment method | |
| JP2007181784A (en) | Waste treatment apparatus | |
| JP3377091B2 (en) | Method and apparatus for treating leachate at landfill site | |
| JP3513120B2 (en) | Treatment of water containing dioxins | |
| JP2003225643A (en) | Apparatus and method for treating organic contaminant | |
| JP3404013B2 (en) | Smoke washing wastewater treatment method and apparatus | |
| JPH11188389A (en) | Method and apparatus for treating seepage water | |
| JP6052041B2 (en) | Waste water treatment method and waste water treatment equipment | |
| JP2007209919A (en) | Salt recovery method and salt recovery apparatus | |
| JP2003266090A (en) | Wastewater treatment method | |
| JP2010194436A (en) | Wastewater treatment method | |
| JP2003103271A (en) | Treatment method for dioxins in wastewater | |
| JP3347673B2 (en) | Waste treatment method | |
| JP3485450B2 (en) | Resource recovery landfill method | |
| JP2003211143A (en) | Device for cleaning soil | |
| WO2007013285A1 (en) | Method of detoxification treatment for filter with persistent substance adhering thereto | |
| JP2008264727A (en) | Method for decomposing hardly decomposable harmful material | |
| JP3268273B2 (en) | Treatment method and treatment device for leachate at final disposal site | |
| JP2004188340A (en) | Method for treating liquid containing dioxins | |
| JP2002028672A (en) | Method and apparatus for treating wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20040106 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20040108 |
|
| R150 | Certificate of patent or registration of utility model |
Ref document number: 3513120 Country of ref document: JP Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090116 Year of fee payment: 5 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20100116 Year of fee payment: 6 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20100116 Year of fee payment: 6 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20100116 Year of fee payment: 6 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20110116 Year of fee payment: 7 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20110116 Year of fee payment: 7 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20120116 Year of fee payment: 8 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20120116 Year of fee payment: 8 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130116 Year of fee payment: 9 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130116 Year of fee payment: 9 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130116 Year of fee payment: 9 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20140116 Year of fee payment: 10 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| LAPS | Cancellation because of no payment of annual fees |