JPH04190833A - Treating method for waster water mixed with organic solvent - Google Patents
Treating method for waster water mixed with organic solventInfo
- Publication number
- JPH04190833A JPH04190833A JP32383190A JP32383190A JPH04190833A JP H04190833 A JPH04190833 A JP H04190833A JP 32383190 A JP32383190 A JP 32383190A JP 32383190 A JP32383190 A JP 32383190A JP H04190833 A JPH04190833 A JP H04190833A
- Authority
- JP
- Japan
- Prior art keywords
- water
- solvent
- organic solvent
- liquid
- phase
- 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.)
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
（産業上の利用分野）
本発明は疎水性有機溶剤を含有する排水から疎水性有機
溶剤を分離して回収する場合に使用する有機溶剤混合排
水の処理方法に関するものである。Detailed Description of the Invention (Field of Industrial Application) The present invention relates to a method for treating organic solvent-mixed wastewater, which is used when separating and recovering hydrophobic organic solvents from wastewater containing hydrophobic organic solvents. be.
（従来の技術）
有機溶剤を含有する排水から、その有機溶剤を分離・回
収する方法として、浸透気化脱法が知られている。この
方法においては、膜の透過側を減圧し、膜内で透過物質
の濃縮を連続的に行い、その透過物質を低い蒸気圧のも
とで蒸発させ、透過物質を気相の状態で分離している。(Prior Art) A pervaporation method is known as a method for separating and recovering organic solvents from wastewater containing them. In this method, the pressure on the permeate side of the membrane is reduced, the permeate substance is continuously concentrated within the membrane, and the permeate substance is evaporated under low vapor pressure to separate the permeate substance in the gas phase. ing.
この方法によれば、非透過物質の蒸発鼠を小さくし得、
それだけ蒸発芹う熱に基づく熱損失を小とてきる。According to this method, the evaporation rate of non-permeable substances can be reduced,
That much reduces heat loss due to evaporative heat.
（解決しようとする課題）
この浸透気化脱法において、分離速度を増大し、大量の
排水の処理を可能とするために、他の分離性との組合せ
が考えられるが、例えば、蒸留法との組合せでは、浸透
気化脱法の利点である省エネルギー性、操作の簡便性等
が喪失されてしまい、不合理である。(Problem to be solved) In order to increase the separation rate and make it possible to treat a large amount of wastewater, this pervaporation desorption method can be combined with other separability methods. For example, combinations with distillation methods can be considered. In this case, the advantages of the pervaporation removal method, such as energy saving and ease of operation, are lost, which is unreasonable.
本発明の目的は、トルエン、キシレン、ヘキサン、ＭＥ
Ｋ等か疎水性有機溶剤であり、その比重差を利用するこ
としこよって小エネルギーで分離できることに着目し、
上記浸透気化脱法と液液槽分離との組合せによって、低
エネルギーで、かつ簡便な操作で排水中からトルエン、
キシレン、ヘキサン、ＭＥＫ等を分離・回収できる有機
溶剤混合排水の処理方法を提供することにある。The purpose of this invention is toluene, xylene, hexane, ME
We focused on the fact that K and other hydrophobic organic solvents can be separated with low energy by utilizing the difference in their specific gravity.
By combining the above-mentioned pervaporation desorption method and liquid-liquid tank separation, toluene can be extracted from wastewater with low energy and simple operation.
The object of the present invention is to provide a method for treating organic solvent-mixed wastewater that can separate and recover xylene, hexane, MEK, etc.
（課題を解決するための手段）
本発明の有機溶剤混合排水の処理方法は、疎水性有機溶
剤を含有する排水を液液分離槽により溶剤相と水相とに
分離したのち、溶剤相は回収し、水相は浸透気化膜モジ
ュールにより分離処理し、溶剤を濃縮した濃縮側は液液
分離４′ｉｌｙ層に戻して循環させ、希釈側は放出する
ことを特徴とする構成である。(Means for Solving the Problems) The method for treating organic solvent mixed wastewater of the present invention involves separating wastewater containing a hydrophobic organic solvent into a solvent phase and an aqueous phase in a liquid-liquid separation tank, and then recovering the solvent phase. However, the aqueous phase is separated by a pervaporation membrane module, the concentrated side where the solvent is concentrated is returned to the liquid-liquid separation layer for circulation, and the diluted side is discharged.
（実施例の説明） 以下、図面により本発明の詳細な説明する。(Explanation of Examples) Hereinafter, the present invention will be explained in detail with reference to the drawings.
第１図は本発明において使用する処理装置の一例を示し
、有機溶剤の沸点が水よりも高い場合に使用される。FIG. 1 shows an example of a treatment apparatus used in the present invention, which is used when the boiling point of the organic solvent is higher than that of water.
第１図において、１は液液分離槽であり、疎水性有機溶
剤を含有する排水が上層の溶剤相と下層の水相とに比重
差によって分離される。２は溶剤回収管である。３は浸
透気化膜モジュールであり、膜には有機溶剤をよく遮断
し、水蒸気を良く透過するものが用いられている。４は
液液分離槽１の水相の水を浸透気化膜モジュール３に供
給する供給ポンプ、５は予熱器、６は加熱媒体循環配管
である。７は浸透気化膜モジュールル３の非透過液を液
液分離槽１に戻すためのリターン管、８は冷却器である
。９は浸透気化膜モジュールル３の透過側を減圧する真
空ポンプ、１０は浸透気化膜モジュールル３と真空ポン
プ９との間に設けた凝縮器、１１は凝縮水放流管、１２
は不凝縮ガス放出管である。In FIG. 1, 1 is a liquid-liquid separation tank, in which waste water containing a hydrophobic organic solvent is separated into an upper solvent phase and a lower aqueous phase based on the difference in specific gravity. 2 is a solvent recovery pipe. 3 is a pervaporation membrane module, and the membrane used is one that blocks organic solvents well and permeates water vapor well. 4 is a supply pump that supplies water in the aqueous phase of the liquid-liquid separation tank 1 to the pervaporation membrane module 3; 5 is a preheater; and 6 is a heating medium circulation pipe. 7 is a return pipe for returning the non-permeated liquid of the pervaporation membrane module 3 to the liquid-liquid separation tank 1, and 8 is a cooler. 9 is a vacuum pump that reduces the pressure on the permeate side of the pervaporation membrane module 3; 10 is a condenser provided between the pervaporation membrane module 3 and the vacuum pump 9; 11 is a condensed water discharge pipe; 12
is a non-condensable gas discharge pipe.
１３は上記冷却器８並びに凝縮器１０に対する冷却媒体
循環配管である。１４は排水供給管であり、冷却器８の
手前においてリターン管７に連結されている。13 is a cooling medium circulation pipe for the cooler 8 and condenser 10. 14 is a wastewater supply pipe, which is connected to the return pipe 7 before the cooler 8.
本発明により、水よりも沸点の高い疎水性有機溶剤、例
えは、トルエン、キシレン等を含有する排水からその有
機溶剤を分離・回収するには、第１図において、排水を
排水供給管１４により冷却器８で冷却しながら液液分離
槽１内に導入する。この液液分離槽１内において、排水
が上層の溶剤相と下層の水相とにその比重差のために分
離される。According to the present invention, in order to separate and recover organic solvents from wastewater containing hydrophobic organic solvents having a boiling point higher than that of water, such as toluene and xylene, the wastewater is connected to a wastewater supply pipe 14 in FIG. The liquid is introduced into the liquid-liquid separation tank 1 while being cooled by a cooler 8. In this liquid-liquid separation tank 1, waste water is separated into an upper solvent phase and a lower aqueous phase due to the difference in specific gravity.
この下層の水相には、操作温度下での平衡溶Ｐｉ量の有
機溶剤が含有されている。上層の溶剤相は排水導入量に
応じ、オーバーフローにより溶剤回収′ｆ２より回収す
る。This lower aqueous phase contains an organic solvent in an amount equal to the equilibrium solution Pi at the operating temperature. The upper solvent phase is recovered from the solvent recovery 'f2 by overflow depending on the amount of water introduced.
この液液分離槽１内の下層の水相を予熱しながら供給ポ
ンプ４によって浸透気化膜モジュール及３内に供給する
と共に真空ポンプ９によって浸透気化膜モジュールル３
の透過側を減圧する。供給水中の水においては、浸透気
化膜モジュールル３の膜での水蒸気に対する選択透過性
のために膜を透過し、その間、透過側の減圧のために蒸
発して水蒸気の気相で透過し、この透過側における有機
溶剤の希釈された水蒸気が凝縮器１０で凝縮されてその
凝縮水が放流管ＩＩより排出され、非凝縮水蒸気が放出
管１２より排出される。The lower aqueous phase in the liquid-liquid separation tank 1 is preheated and supplied into the pervaporation membrane module 3 by the supply pump 4, and at the same time by the vacuum pump 9.
Reduce the pressure on the permeate side. In the water in the feed water, it permeates through the membrane due to the selective permeability to water vapor in the membrane of the pervaporation membrane module 3, while it evaporates due to the reduced pressure on the permeate side and permeates in the gas phase of water vapor. The diluted water vapor of the organic solvent on the permeation side is condensed in the condenser 10, the condensed water is discharged from the discharge pipe II, and the non-condensed water vapor is discharged from the discharge pipe 12.
他方、非透過側においては、溶剤か濃縮され、この濃縮
水をリターン管７を経て冷却器８で冷却のうえ、液液分
離槽１に戻し、以後、以上を１サイクルとしてリサイク
ルさせていく。On the other hand, on the non-permeate side, the solvent is concentrated, and this concentrated water is cooled by the cooler 8 through the return pipe 7, and then returned to the liquid-liquid separation tank 1, whereupon the above is recycled as one cycle.
第２図は本発明において使用する処理装置の別個を示し
、疎水性有機溶剤の沸点が水よりも低い場合に使用され
る。FIG. 2 shows a separate treatment apparatus used in the present invention, which is used when the boiling point of the hydrophobic organic solvent is lower than that of water.
第２図において、１は液液分ｉｔ槽を、２は溶剤回収管
を、４は供給ポンプを、５は予熱器を、６は加熱媒体循
環配管をそれぞれ示している。３は浸透気化膜モジュー
ルを示し、膜には有機溶剤に対して選択透過性を有する
ものが使用されている。In FIG. 2, 1 indicates a liquid-liquid separation IT tank, 2 a solvent recovery pipe, 4 a supply pump, 5 a preheater, and 6 a heating medium circulation pipe. Reference numeral 3 indicates a pervaporation membrane module, in which a membrane having selective permselectivity for organic solvents is used.
１１は非透過水排出管である。９は真空ポンプを、１０
は凝縮器を、１２０は不凝縮ガス排出管をそれぞれ示し
ている。、７は浸透気化膜モジュールル３の透過有機溶
剤蒸気の凝縮液を液液分離槽１に戻すためのリターン管
である。８は冷却器、１３は上記冷却器８並びに凝縮器
１０に対する冷却媒体循環配管である。１４は排水供給
管であり、冷却器８の手前においてリターン管７に連結
されている。11 is a non-permeable water discharge pipe. 9 is the vacuum pump, 10 is
120 indicates a condenser, and 120 indicates a non-condensable gas discharge pipe. , 7 are return pipes for returning the condensate of permeated organic solvent vapor from the pervaporation membrane module 3 to the liquid-liquid separation tank 1. 8 is a cooler; 13 is a cooling medium circulation pipe for the cooler 8 and condenser 10; 14 is a wastewater supply pipe, which is connected to the return pipe 7 before the cooler 8.
上記第２図に示す処理装置を使用して本発明により、水
よりも沸点の低い疎水性有機溶剤、例えば、ヘキサン、
ＭＥＫ等を含有する排水からその有機溶剤を分離・回収
するには、第２図において、排水を排水供給管１４によ
り冷却器８て冷却しながら液液分離槽１内に導入し、こ
の液液分離槽１内の上層の溶剤相を排水導入量に応じ、
オーバーフローにより溶剤回収管２より回収しつつ、液
液分離槽１内の下層の水相を予熱しながら供給ポンプ４
によって浸透気化膜モジユール３内に供給すると共に真
空ポンプ９によって浸透気化膜モジュール３の透過側を
減圧する。供給水中の有機溶剤においては、浸透気化膜
モジュール３の膜での有機溶剤蒸気に対する選択透過性
のために膜を透過し、その間、透過側の減圧のために蒸
発して有機溶剤蒸気の気相で透過し、この有機溶剤の透
過・分離により有機溶剤の希釈された非透過側の水が放
流管１１より排出される。他方、透過側における有機溶
剤蒸気が凝縮器１０で凝縮されてその凝縮有機溶剤がリ
ターン管７を経て冷却器８で冷却のうえ、液液分離槽１
に戻し、非凝縮ガスは放出管１２０から排出し、以後、
以上を１サイクルとしてリサイクルさせていく。According to the present invention, a hydrophobic organic solvent having a boiling point lower than that of water, such as hexane,
In order to separate and recover organic solvents from wastewater containing MEK, etc., in FIG. The upper solvent phase in separation tank 1 is adjusted according to the amount of wastewater introduced.
The supply pump 4 is preheating the lower aqueous phase in the liquid-liquid separation tank 1 while collecting it from the solvent recovery pipe 2 due to overflow.
The gas is supplied into the pervaporation membrane module 3 by the vacuum pump 9, and the permeate side of the pervaporation membrane module 3 is depressurized by the vacuum pump 9. The organic solvent in the feed water permeates through the membrane due to the selective permeability to the organic solvent vapor in the membrane of the pervaporation membrane module 3, and during that time, it evaporates due to the reduced pressure on the permeate side, resulting in a gas phase of the organic solvent vapor. Through the permeation and separation of the organic solvent, the water on the non-permeate side where the organic solvent is diluted is discharged from the discharge pipe 11. On the other hand, the organic solvent vapor on the permeation side is condensed in the condenser 10, and the condensed organic solvent passes through the return pipe 7, is cooled in the cooler 8, and is then transferred to the liquid-liquid separation tank 1.
, the non-condensable gas is discharged from the discharge pipe 120, and thereafter,
The above steps are recycled as one cycle.
上記において、浸透気化膜モジュール３の膜は、水蒸気
又は有機溶剤蒸気に対する選択透過性に応じて選択され
る。例えば、トルエン蒸気に対し選択透過性を有する膜
としては、シリコンゴム系ポリイミド膜が選択される。In the above, the membrane of the pervaporation membrane module 3 is selected depending on the permselectivity to water vapor or organic solvent vapor. For example, a silicone rubber-based polyimide membrane is selected as the membrane having selective permeability to toluene vapor.
又、浸透気化膜モジュールの形式としては、スパイラル
型、中空糸型、管状型、プレート型等が使用される。Further, as the format of the pervaporation membrane module, spiral type, hollow fiber type, tubular type, plate type, etc. are used.
本発明の疎水性有機溶剤混合排水の処理方法は、浸透気
化膜性と液液分離槽法との結合であって、共に低エネル
ギーによって操作できるから、全体としての使用エネル
ギーを充分に小さくできる。The method for treating hydrophobic organic solvent-mixed wastewater of the present invention combines the pervaporation membrane method and the liquid-liquid separation tank method, and both can be operated with low energy, so the overall energy consumption can be sufficiently reduced.
このことは次ぎの実施例からも明かである。This is clear from the following examples.
実施例
排水としてはトルエン／水の混合比が１／９９のトルエ
ン含有Ｊ１水を使用し、処理装置には第２図に示すもの
を使用した。浸透気化膜モジュール３には、シリコンゴ
ム系ポリイミド膜を用いた膜面積１４ｍ２のスパイラル
型浸透気化膜モジュールを使用した。As the example wastewater, toluene-containing J1 water with a toluene/water mixing ratio of 1/99 was used, and the treatment device shown in FIG. 2 was used. As the pervaporation membrane module 3, a spiral type pervaporation membrane module using a silicone rubber-based polyimide membrane and having a membrane area of 14 m2 was used.
排水供給量は流量３０ｋｇ／ｈｒとし、冷却器８で２０
°Ｃ以下に冷却して液液分離槽１内に導入した。この場
合の下層の水相のトルエン平衡溶解濃度は０ 、０４５
ｗ ｔ％であった。供給ポンプ４による供給流量は３
００ ｋ ｇ ／ ｈ ｒどし、予熱語５による予熱温
度は６０’Ｃとした。浸透気化膜モジュール３での非透
過側の放流管１１による放流量を約３０ｋｇ／ｈｒとし
、リターン管７による循環流量を２７０ｋｇ／ｈｒとし
た。非透過側の放流水中のトルエン濃度は０．０１ｗｔ
％であり、循憚側のトルエン濃度は０．０４９％であっ
た。The amount of waste water supplied is 30 kg/hr, and the flow rate is 20 kg/hr with cooler 8.
The mixture was cooled to below .degree. C. and introduced into the liquid-liquid separation tank 1. In this case, the equilibrium dissolved concentration of toluene in the lower aqueous phase is 0,045
It was wt%. The supply flow rate by supply pump 4 is 3
00 kg/hr, and the preheating temperature according to preheating word 5 was 60'C. The discharge amount through the discharge pipe 11 on the non-permeate side of the pervaporation membrane module 3 was approximately 30 kg/hr, and the circulation flow rate through the return pipe 7 was approximately 270 kg/hr. The toluene concentration in the effluent on the non-permeable side is 0.01wt.
%, and the toluene concentration on the circulating side was 0.049%.
この場合の所要運転エネルギーは１８０００Ｋｃａｌ／
ｈｒであった。これに対して上記排水を上記と同一の放
流排水条件（放流量：約３０ｋｇ／ｈｒ、トルエン濃度
：Ｏ，００１ｗｔ％）で処理するのに必要なエネルギー
は約２３０００Ｋｃａｌ／ｈｒである。The required operating energy in this case is 18,000 Kcal/
It was hr. On the other hand, the energy required to treat the waste water under the same discharge conditions as above (discharge rate: about 30 kg/hr, toluene concentration: O,001 wt%) is about 23,000 Kcal/hr.
（発明の効果）
本発明の有機溶剤混合排水の処理方法においては、上述
した通り、疎水性有機溶剤を含有する排水を比重差を利
用して水相と溶剤相とに分離したうえで、溶剤濃度の希
釈された水相を浸透気化膜性で処理しており、比重差を
利用しての液液槽分離に必要なエネルギーは、水相にお
ける有機溶剤の平衡溶解量を低くするための冷却に対す
る冷却媒体の循環エネルギーだけであって、上記液液槽
分離並びに浸透気化膜分離を共に低エネルギーで操作で
きるから、エネルギーの省力化を良く達成できる。又、
比重差を利用しての液液槽分離が自然分離であるから、
浸透気化脱法単独の場合と実質上、操作の異なるところ
がなく、浸透気化脱法ｍ独の場合と同様、操作が簡便で
ある。従って。(Effects of the Invention) As described above, in the method for treating organic solvent-mixed wastewater of the present invention, wastewater containing a hydrophobic organic solvent is separated into an aqueous phase and a solvent phase using the difference in specific gravity, and then the solvent is The diluted aqueous phase is treated by pervaporation membrane, and the energy required for liquid-liquid tank separation using the difference in specific gravity is reduced by cooling to lower the equilibrium dissolution amount of organic solvent in the aqueous phase. Since both the liquid-liquid tank separation and pervaporation membrane separation can be operated with low energy using only the circulating energy of the cooling medium, energy savings can be achieved well. or,
Since liquid-liquid tank separation using the difference in specific gravity is natural separation,
There is virtually no difference in operation from the case of pervaporation removal alone, and the operation is simple as in the case of pervaporation removal. Therefore.
本発明によれば、浸透気化膜性の省エネルギー性、操作
の簡便性を充分に保有して、疎水性有機溶剤を含有する
排水を高速度で処理することが可能となる。According to the present invention, it is possible to treat wastewater containing a hydrophobic organic solvent at high speed while fully retaining the energy saving properties and operational simplicity of pervaporation membrane properties.
第１図並びに第２図は本発明において使用する異なる処
理装置を示す説明図である。
１・・・液液分離漕、２・・有機溶剤回収管、３・・浸
透気化膜モジュール、４・供給ポンプ、７−・・リター
ン管、８・・冷却器、９・・・真空ポンプ、１０・・・
凝縮器、１４・・・排水供給管。FIG. 1 and FIG. 2 are explanatory diagrams showing different processing devices used in the present invention. DESCRIPTION OF SYMBOLS 1...Liquid-liquid separation tank, 2...Organic solvent recovery pipe, 3...Pervaporation membrane module, 4-Supply pump, 7-...Return pipe, 8...Cooler, 9...Vacuum pump, 10...
Condenser, 14...Drainage supply pipe.
Claims (1)
相と水相とに分離したのち、溶剤相は回収し、水相は浸
透気化膜モジュールにより分離処理し、溶剤を濃縮した
濃縮側は液液分離槽に戻して循環させ、希釈側は放出す
ることを特徴とする有機溶剤混合排水の処理方法。After the wastewater containing hydrophobic organic solvents is separated into a solvent phase and an aqueous phase using a liquid-liquid separation tank, the solvent phase is recovered, the aqueous phase is separated using a pervaporation membrane module, and the concentration side where the solvent is concentrated is A method for treating organic solvent mixed wastewater, characterized by returning it to a liquid-liquid separation tank and circulating it, and discharging the diluted side.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2323831A JPH0736887B2 (en) | 1990-11-26 | 1990-11-26 | Wastewater treatment equipment mixed with organic solvents |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2323831A JPH0736887B2 (en) | 1990-11-26 | 1990-11-26 | Wastewater treatment equipment mixed with organic solvents |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04190833A true JPH04190833A (en) | 1992-07-09 |
| JPH0736887B2 JPH0736887B2 (en) | 1995-04-26 |
Family
ID=18159084
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2323831A Expired - Lifetime JPH0736887B2 (en) | 1990-11-26 | 1990-11-26 | Wastewater treatment equipment mixed with organic solvents |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0736887B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5556539A (en) * | 1993-02-26 | 1996-09-17 | Mitsubishi Chemical Corporation | Apparatus for separating a liquid mixture by pervaporation |
| CN103752173A (en) * | 2014-01-22 | 2014-04-30 | 清华大学 | Frequent flow direction switching type membrane distillation system |
| CN115140881A (en) * | 2022-07-08 | 2022-10-04 | 上海电气集团股份有限公司 | Organic wastewater treatment system and treatment process |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5712882A (en) * | 1980-06-26 | 1982-01-22 | Mitsubishi Heavy Ind Ltd | Recovery of water by-produced in synthesis of aromatic hydrocarbon mixture |
| JPS58501110A (en) * | 1981-06-17 | 1983-07-14 | テキサス ロメツク インコ−ポレ−テツド | Method and apparatus for regenerating useful water and other materials from oil field mud/drainage pits |
| JPS61125407A (en) * | 1984-11-23 | 1986-06-13 | Toyota Motor Corp | Method and apparatus for regenerating washing liquid |
-
1990
- 1990-11-26 JP JP2323831A patent/JPH0736887B2/en not_active Expired - Lifetime
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5712882A (en) * | 1980-06-26 | 1982-01-22 | Mitsubishi Heavy Ind Ltd | Recovery of water by-produced in synthesis of aromatic hydrocarbon mixture |
| JPS58501110A (en) * | 1981-06-17 | 1983-07-14 | テキサス ロメツク インコ−ポレ−テツド | Method and apparatus for regenerating useful water and other materials from oil field mud/drainage pits |
| JPS61125407A (en) * | 1984-11-23 | 1986-06-13 | Toyota Motor Corp | Method and apparatus for regenerating washing liquid |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5556539A (en) * | 1993-02-26 | 1996-09-17 | Mitsubishi Chemical Corporation | Apparatus for separating a liquid mixture by pervaporation |
| US5582721A (en) * | 1993-02-26 | 1996-12-10 | Mitsubishi Chemical Corporation | Apparatus for separating a liquid mixture |
| CN103752173A (en) * | 2014-01-22 | 2014-04-30 | 清华大学 | Frequent flow direction switching type membrane distillation system |
| CN115140881A (en) * | 2022-07-08 | 2022-10-04 | 上海电气集团股份有限公司 | Organic wastewater treatment system and treatment process |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0736887B2 (en) | 1995-04-26 |
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