JP2775789B2 - Wastewater treatment method - Google Patents
Wastewater treatment methodInfo
- Publication number
- JP2775789B2 JP2775789B2 JP63323043A JP32304388A JP2775789B2 JP 2775789 B2 JP2775789 B2 JP 2775789B2 JP 63323043 A JP63323043 A JP 63323043A JP 32304388 A JP32304388 A JP 32304388A JP 2775789 B2 JP2775789 B2 JP 2775789B2
- Authority
- JP
- Japan
- Prior art keywords
- solvent
- wastewater
- aeration
- heat
- wastewater treatment
- 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 Gases By Adsorption (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Physical Water Treatments (AREA)
Description
【発明の詳細な説明】 （産業上の利用分野） 本発明は溶剤を含有する排水を低コストにて浄化する
排水処理方法に関し、特に吸着剤等を用いた溶剤回収装
置から排出される含溶剤排水を浄化する排水処理方法に
関するものである。Description: TECHNICAL FIELD The present invention relates to a wastewater treatment method for purifying wastewater containing a solvent at low cost, and in particular, a solvent-containing wastewater discharged from a solvent recovery device using an adsorbent or the like. The present invention relates to a wastewater treatment method for purifying wastewater.
（従来の技術） 一般に溶剤を含有する排気ガスから溶剤を回収する溶
剤回収装置としては活性炭等で溶剤を吸着し、その吸着
された溶剤を水蒸気にて脱着し、活性炭等を再生して処
理される吸着脱着操作方法が広く採られているが、この
溶剤回収装置からは溶剤を含む排水が出ることは必至で
ある。従来、水に溶けにくい溶剤を先の溶剤回収装置に
て回収した際には回収装置からの排水には微量の溶剤が
含まれるがこの排水を浄化する方法としては、例えば第
２図に示した特開昭51-16282なる方法即ちエアレーショ
ンによる排水浄化方法が知られている。しかしながら特
開昭51-16282に記載されている方法では、排水中に多量
の溶剤が含まれる場合、もしくは溶剤の沸点が高い場合
において常温のエアレーション操作にて排水中の溶剤濃
度を充分に下げるためには、処理時間が大幅に長くな
る、もしくは処理装置が非常に大きくなるという欠点が
あった。また近年問題となっているトリクロルエチレン
等の塩素系有機溶剤等を対象とした際には非常に高度の
排水処理が必要であるが、これらに対して、常温のエア
レーション操作にて対処した際には、前記同様排水の処
理時間が大幅に長くなる、もしくは処理装置が非常に大
きくなるという欠点があった。これらの欠点を解決する
方法としては、処理温度即ち処理される排水温度を上げ
る方法即ち加熱エアレーション方法が知られている。加
熱エアレーション方法における処理方法のフローの１例
を第３図に示す。しかしながら、エタノール等の比較的
沸点の高い水溶性の溶剤を含有する排水もしくは高度の
排水処理が要求されるトリクロルエチレン等の塩素系有
機溶剤を含む排水等を加熱エアレーション方法にて浄化
するには排水を高温にて処理する必要があるために多量
の熱が必要であり、排水処理装置のランニングコストが
非常に大きくなるという欠点があった。(Prior art) In general, a solvent recovery device for recovering a solvent from exhaust gas containing the solvent is treated by adsorbing the solvent with activated carbon or the like, desorbing the adsorbed solvent with steam, and regenerating the activated carbon or the like. Although the adsorption / desorption operation method is widely used, it is inevitable that wastewater containing the solvent is discharged from the solvent recovery device. Conventionally, when a solvent that is hardly soluble in water is recovered by the above-mentioned solvent recovery device, a small amount of solvent is contained in the wastewater from the recovery device. As a method for purifying this wastewater, for example, as shown in FIG. A method disclosed in Japanese Patent Application Laid-Open No. S51-16282, that is, a method of purifying wastewater by aeration is known. However, in the method described in JP-A-51-16282, when a large amount of solvent is contained in the wastewater, or when the boiling point of the solvent is high, the concentration of the solvent in the wastewater is sufficiently reduced by aeration operation at normal temperature. Has a drawback that the processing time is significantly increased or the processing apparatus becomes very large. In addition, when targeting chlorine-based organic solvents such as trichloroethylene, which has become a problem in recent years, very high-level wastewater treatment is required, but when these are dealt with by normal temperature aeration operation, However, as described above, there is a disadvantage that the treatment time of the wastewater is greatly lengthened, or the size of the treatment device becomes very large. As a method for solving these drawbacks, there is known a method of increasing the processing temperature, that is, the temperature of the waste water to be treated, that is, a heating aeration method. FIG. 3 shows an example of the flow of the processing method in the heating aeration method. However, to purify wastewater containing a water-soluble solvent having a relatively high boiling point such as ethanol or chlorinated organic solvent such as trichloroethylene which requires high-level wastewater treatment by a heated aeration method, Has to be treated at a high temperature, so that a large amount of heat is required, and the running cost of the wastewater treatment apparatus becomes very large.
（発明が解決しようとする課題点） 本発明の目的は、溶剤回収装置から排出される含溶剤
排水をエアレーション操作にて浄化する排水処理方法で
あって、前記従来の欠点即ち、エタノール等の比較的沸
点の高い水溶性の溶剤を含有する排水もしくは高度の排
水処理が要求されるトリクロルエチレン等の塩素系有機
溶剤を含む排水等を加熱エアレーション法にて浄化した
際、この排水浄化方法では多量の熱が必要で膨大なラン
ニングコストがかかるという欠点を解消し、排水を浄化
するランニングコストを大幅に低減させる排水処理方法
を提供せんとするものである。(Problems to be Solved by the Invention) An object of the present invention is a wastewater treatment method for purifying a solvent-containing wastewater discharged from a solvent recovery device by an aeration operation. When purifying wastewater containing a water-soluble solvent with a high boiling point or wastewater containing a chlorinated organic solvent such as trichlorethylene, which requires advanced wastewater treatment, by a heated aeration method, this wastewater purification method requires a large amount of water. An object of the present invention is to provide a wastewater treatment method that solves the drawback that heat is required and requires enormous running costs, and greatly reduces the running costs for purifying wastewater.
（問題点を解決するための手段） 即ち本発明は、有機溶剤、とくに水溶性の有機溶剤を
含む排気ガスから該有機溶剤を活性炭等の吸着剤を用い
た溶剤回収装置にて回収する際に該吸着剤の再生に加熱
水蒸気を使用した場合に生ずる該有機溶剤を含有する排
水に対し、該排水を加熱し併せて該排水に空気を供給し
即ち加熱エアレーションにより該排水中の該有機溶剤を
除去する排水処理方法であって、該溶剤回収装置の再生
時に生ずる水蒸気と該溶剤の混合ガス（以下脱着ガス）
が持つ熱を熱交換器により回収し、該脱着ガスから回収
された熱を該排水処理装置（エアレーション槽）の加熱
源に用いることを特徴とする排水処理方法である。(Means for Solving the Problems) That is, the present invention relates to a method for recovering an organic solvent from an exhaust gas containing an organic solvent, particularly a water-soluble organic solvent, using a solvent recovery device using an adsorbent such as activated carbon. For wastewater containing the organic solvent generated when heated steam is used for regeneration of the adsorbent, the wastewater is heated and air is supplied to the wastewater, that is, the organic solvent in the wastewater is heated by aeration. A wastewater treatment method for removing water, wherein a mixed gas of steam and the solvent generated during regeneration of the solvent recovery device (hereinafter, desorbed gas)
A wastewater treatment method characterized by using a heat exchanger to recover heat of the wastewater and using the heat recovered from the desorbed gas as a heating source of the wastewater treatment device (aeration tank).
本発明においては、前記熱交換器はエアレーション槽
の内部に設置されるのが望ましいが、外部にあってもよ
いことはもちろんである。In the present invention, it is desirable that the heat exchanger is installed inside the aeration tank, but it goes without saying that it may be outside.
以下、この発明の詳細を第１図に示すフローシートに
基づいて説明する。Hereinafter, the details of the present invention will be described based on the flow sheet shown in FIG.
溶剤の蒸気を含むガスを、管１に通じブロワー２を介
して、吸着塔３に送り込むと、同塔３内に充填されてい
る活性炭等の吸着剤が、原ガス中の溶剤を吸着する。原
ガスは溶剤が除去されることにより浄化され大気中に排
出される。溶剤で飽和した先の吸着剤を再生するために
吸着操作を脱着操作に手動あるいは自動で切り替える。
即ち脱着用の水蒸気を吸着塔に供給する。When a gas containing a solvent vapor passes through the pipe 1 and is sent to the adsorption tower 3 through the blower 2, the adsorbent such as activated carbon filled in the tower 3 adsorbs the solvent in the raw gas. The raw gas is purified by removing the solvent and discharged to the atmosphere. The adsorption operation is manually or automatically switched to the desorption operation in order to regenerate the adsorbent saturated with the solvent.
That is, the steam for desorption is supplied to the adsorption tower.
吸着剤を再生するために吸着塔３に供給された水蒸気
は吸着剤に吸着した溶剤を脱着し、溶剤と水蒸気の混合
ガス、即ち脱着ガスとなり管４を通じエアレーションタ
ンク７内の熱交換器13に送られ、エアレーションタンク
７内の被処理水と熱交換され被処理水を加熱する。脱着
ガスの内、凝縮しなかった脱着ガスについては管12を通
じコンデンサー５に送られそこで凝縮されたのち、凝縮
液はセパレータ６に供給され、そこで比重差を利用して
溶剤層6aと水層6bに分離される、熱交換器13を通じた脱
着ガスの内の凝縮した液は管14を通じセパレータ６に送
られ、同様溶剤層6aと水層6bに分離される。溶剤層6aは
回収溶剤として外部に抜き出す。The water vapor supplied to the adsorption tower 3 for regenerating the adsorbent desorbs the solvent adsorbed on the adsorbent and becomes a mixed gas of the solvent and water vapor, that is, a desorbed gas, through the pipe 4 to the heat exchanger 13 in the aeration tank 7. The heat is exchanged with the water to be treated in the aeration tank 7 to heat the water to be treated. Among the desorbed gases, the desorbed gas that has not been condensed is sent to the condenser 5 through the pipe 12 and condensed there, and then the condensed liquid is supplied to the separator 6, where the solvent layer 6a and the aqueous layer 6b are utilized by utilizing the specific gravity difference. The condensed liquid in the desorbed gas passed through the heat exchanger 13 is sent to the separator 6 through the pipe 14, and is similarly separated into the solvent layer 6a and the water layer 6b. The solvent layer 6a is extracted to the outside as a recovered solvent.
発明の処理対象となる含溶剤排水、即ち水層6bはポン
プ15等によりエアレーションタンク７に供給されエアレ
ーションタンク内の熱交換器13により加熱され、さらに
エアレーションタンク７に供給されるガスにより水層7b
に溶解している溶剤を外層7aに放出される。エアレーシ
ョンタンク７に供給するガスは空気が適当であるが、原
ガスを用いることも可能である。即ち吸着塔３の手前か
らバイパス管８を分岐させ、エアレーションタンク７に
原ガスを供給すればよい。The solvent-containing wastewater to be treated in the present invention, that is, the water layer 6b is supplied to the aeration tank 7 by the pump 15 or the like, heated by the heat exchanger 13 in the aeration tank, and further supplied to the aeration tank 7 by the gas supplied to the aeration tank 7.
Is dissolved in the outer layer 7a. The gas supplied to the aeration tank 7 is suitably air, but it is also possible to use raw gas. That is, the bypass pipe 8 may be branched from just before the adsorption tower 3, and the raw gas may be supplied to the aeration tank 7.
これらの処理方法により水層7bの溶剤濃度は著しく低
下し、そのまま下水等に流すことが可能である。With these treatment methods, the solvent concentration of the aqueous layer 7b is significantly reduced, and the aqueous layer 7b can be directly passed to sewage or the like.
気層7aについては水層7bの溶剤濃度が低い場合にはエ
アレーションタンク５とブロワー２前段の管１と、この
両者を結ぶ戻し管10を通じて、排出ガスをブロワー２に
送り込み吸着塔３にて吸着させることができる。また気
層7aの溶剤濃度が高い場合もしくは溶剤濃度が無限大に
発散する場合においては、気層7bは何らかの排気ガス処
理装置16にて処理されることが公害対策上望ましい。For the gas layer 7a, when the solvent concentration of the water layer 7b is low, the exhaust gas is sent to the blower 2 through the aeration tank 5 and the pipe 1 in the preceding stage of the blower 2 and the return pipe 10 connecting the two, and is adsorbed by the adsorption tower 3. Can be done. In addition, when the solvent concentration of the gas layer 7a is high or the solvent concentration diverges to infinity, it is desirable that the gas layer 7b be treated by an exhaust gas treatment device 16 in view of pollution control.
尚、第１図に示したフローシートは本発明の一実施例
にすぎず、要旨を変えない範囲で種々変形して実施する
ことができる。また本発明は溶剤回収装置、及びエアレ
ーション方法についても特に限定するものではない。即
ち溶剤回収装置としては、固定床型、流動層型、回転
型、等の水蒸気脱着を用いた溶剤回収装置が対象とな
る。またエアレーション方法については、第１図に示し
たような１槽式連続エアレーション方式に限らず、多槽
式連続エアレーション方式、もしくはバッチ型エアレー
ション方式などが挙げられる。It should be noted that the flow sheet shown in FIG. 1 is merely an embodiment of the present invention, and can be variously modified and implemented without changing the gist. Further, the present invention does not particularly limit the solvent recovery device and the aeration method. That is, as a solvent recovery apparatus, a solvent recovery apparatus using steam desorption such as a fixed bed type, a fluidized bed type, a rotary type, etc. is an object. The aeration method is not limited to the single-tank continuous aeration method as shown in FIG. 1, but may be a multi-tank continuous aeration method, a batch aeration method, or the like.
第１図に示した、熱交換器については金属性の蛇管も
しくは直管が適当と思われるが、特にこれらを限定する
ものではない。またこれらの熱交換器の伝熱面積等の交
換熱量を規定する数値については、処理される排水の濃
度または必要とされる処理の度合いによりそれぞれ決定
される。As for the heat exchanger shown in FIG. 1, a metallic coiled tube or straight tube is considered to be suitable, but these are not particularly limited. Numerical values defining heat exchange areas such as the heat transfer area of these heat exchangers are determined depending on the concentration of wastewater to be treated or the required degree of treatment.
上記した方法により溶剤回収装置から排出された排水
を加熱エアレーション方式にて浄化する際の熱源として
脱着ガスの潜熱及び顕熱をエアレーションタンク内で回
収することで、排水の浄化にかかるランニングコストを
大幅に低減することが可能となった。By recovering the latent heat and sensible heat of the desorbed gas in the aeration tank as a heat source when purifying the wastewater discharged from the solvent recovery device by the heating aeration method by the above method, the running cost for purifying the wastewater is greatly increased. It became possible to reduce to.
（実施例） 実施例１ 溶剤回収装置から排出されるエタノールを２％含有す
る20kg/hrの排水をバッチ式加熱エアレーションにより
排水中のエタノール濃度を10ppm以下とするためには、
従来の方法即ち排水の加熱源に新たなる水蒸気を用いた
際には10kg/hrの水蒸気が新たに必要であったが、本発
明（第１図）によれば排水の加熱源に溶剤回収装置の脱
着ガスの熱を回収し用いることで新たなる熱源を用いる
ことなく、排水を浄化でき、排水浄化にかかるランニン
グコストのうち排水の加熱にかかるコストをほぼ100％
カットすることができた。(Example) Example 1 In order to reduce the ethanol concentration in the wastewater of 10 kg or less to 20 kg / hr wastewater containing 2% of ethanol discharged from the solvent recovery device by batch heating aeration,
According to the conventional method, that is, a new steam of 10 kg / hr was required when a new steam was used as the heating source of the waste water. According to the present invention (FIG. 1), the solvent recovery device was used as the heating source of the waste water. By collecting and using the heat of the desorbed gas, the wastewater can be purified without using a new heat source.
I was able to cut.
実施例２ 溶剤回収装置から排出されるエタノールを２％含有す
る20kg/hrの排水をバッチ式加熱エアレーションにより
排水中のエタノール濃度を10ppm以下とするためには、
従来の方法即ち排水の加熱源に水蒸気を用いた際には10
kg/hrの水蒸気が新たに必要であったが、本発明の脱着
スチームの潜熱及び顕熱をエアレーションタンクの外部
熱交換器により回収する方法においては、排水処理に新
たに約2.5kg/hrの水蒸気を使用するだけで排水を浄化で
き、排水浄化にかかるランニングコストのうち、排水の
加熱にかかるコストを従来の約75％カットすることがで
きた。Example 2 In order to reduce the concentration of ethanol in wastewater of 10 kg or less to 20 kg / hr wastewater containing 2% of ethanol discharged from the solvent recovery device by batch heating aeration,
In the conventional method, that is, when steam is used
Although kg / hr of steam was newly required, in the method of the present invention for recovering the latent heat and sensible heat of the desorbed steam by the external heat exchanger of the aeration tank, about 2.5 kg / hr was newly added to the wastewater treatment. The wastewater can be purified only by using steam, and of the running costs involved in purifying the wastewater, the cost involved in heating the wastewater has been reduced by about 75% compared to the past.
（発明の効果） 本発明によれば、次のような格別優れた効果が得られ
る。(Effects of the Invention) According to the present invention, the following excellent effects can be obtained.
（１）溶剤回収装置から排出される含有機溶剤排水を加
熱エアレーションにより処理する際の処理にかかるラン
ニングコストを大幅に低減することができる。(1) It is possible to greatly reduce the running cost required for treating the solvent wastewater discharged from the solvent recovery device when the solvent wastewater is treated by heating aeration.
（２）低コストにて高温加熱エアレーション処理が可能
となるため高度の排水処理が可能となる。(2) Since high-temperature heating aeration can be performed at low cost, advanced wastewater treatment can be performed.
第１図は本発明における、溶剤回収装置からの排水を処
理する方法の１例である。 第２図は従来からある、溶剤回収装置の排水をエアレー
ションにより処理した方法の１例であり、第３図は従来
からある、溶剤回収装置の排水を加熱エアレーションに
より処理した方法の１例である。FIG. 1 is an example of a method for treating wastewater from a solvent recovery apparatus according to the present invention. FIG. 2 shows an example of a conventional method of treating waste water of a solvent recovery device by aeration, and FIG. 3 shows an example of a conventional method of treating waste water of a solvent recovery device by heating aeration. .
フロントページの続き (58)調査した分野(Int.Cl.6，ＤＢ名) C02F 1/04 - 1/18 B01D 53/04Continuation of front page (58) Field surveyed (Int.Cl. 6 , DB name) C02F 1/04-1/18 B01D 53/04
Claims (2)
吸着させ、この溶剤を水蒸気により脱着して得た溶剤含
有水蒸気を凝縮し、比重差により溶剤を分離した排水を
エアレーションタンクに入れ、空気によりエアレーショ
ン処理する排水処理方法であって、前記溶剤含有水蒸気
の潜熱又は顕熱を前記エアレーションタンク内の排水の
加熱源として使用することを特徴とする排水処理方法。1. A solvent-containing gas is brought into contact with an adsorbent to adsorb the solvent, the solvent-containing water vapor obtained by desorbing the solvent with water vapor is condensed, and the waste water from which the solvent has been separated by a specific gravity difference is put into an aeration tank. A wastewater treatment method comprising aeration treatment with air, wherein the latent heat or sensible heat of the solvent-containing steam is used as a heating source for wastewater in the aeration tank.
すことにより、前記溶剤含有水蒸気の潜熱又は顕熱を前
記エアレーションタンク内の排水の加熱源として使用す
ることを特徴とする請求項１に記載の排水処理方法。2. The method according to claim 1, wherein said solvent-containing steam is passed through a heat exchanger so that latent heat or sensible heat of said solvent-containing steam is used as a heating source for drainage in said aeration tank. A wastewater treatment method according to item 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63323043A JP2775789B2 (en) | 1988-12-20 | 1988-12-20 | Wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63323043A JP2775789B2 (en) | 1988-12-20 | 1988-12-20 | Wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02169085A JPH02169085A (en) | 1990-06-29 |
| JP2775789B2 true JP2775789B2 (en) | 1998-07-16 |
Family
ID=18150472
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63323043A Expired - Fee Related JP2775789B2 (en) | 1988-12-20 | 1988-12-20 | Wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2775789B2 (en) |
Cited By (1)
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| CN101898071B (en) * | 2009-05-25 | 2012-09-12 | 中国石油化工股份有限公司 | Method for treating sulfur- and hydrocarbon-containing foul waste gas |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2564865Y2 (en) * | 1991-09-10 | 1998-03-11 | オルガノ株式会社 | Purification equipment for water containing organic solvents |
| CN104436988A (en) * | 2013-09-13 | 2015-03-25 | 中国科学院兰州化学物理研究所 | Industrial organic waste gas treatment and cleaning process |
| CN105570906B (en) * | 2016-02-22 | 2018-05-29 | 浙江尚鼎工业炉有限公司 | A kind of castoff processing system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52146775A (en) * | 1976-06-02 | 1977-12-06 | Mitsubishi Heavy Ind Ltd | Heat recovery in separation process of mixed gases |
| JPS52146776A (en) * | 1976-06-02 | 1977-12-06 | Mitsubishi Heavy Ind Ltd | Recovery of sovent vapor |
-
1988
- 1988-12-20 JP JP63323043A patent/JP2775789B2/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101898071B (en) * | 2009-05-25 | 2012-09-12 | 中国石油化工股份有限公司 | Method for treating sulfur- and hydrocarbon-containing foul waste gas |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH02169085A (en) | 1990-06-29 |
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| LAPS | Cancellation because of no payment of annual fees |