JPH06296831A - Treatment of phenol containing waste water - Google Patents
Treatment of phenol containing waste waterInfo
- Publication number
- JPH06296831A JPH06296831A JP5088769A JP8876993A JPH06296831A JP H06296831 A JPH06296831 A JP H06296831A JP 5088769 A JP5088769 A JP 5088769A JP 8876993 A JP8876993 A JP 8876993A JP H06296831 A JPH06296831 A JP H06296831A
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- JP
- Japan
- Prior art keywords
- phenol
- membrane
- waste water
- water
- supplied
- 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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Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明はフェノール含有排水から
フェノールを分離、回収する方法に関する。FIELD OF THE INVENTION The present invention relates to a method for separating and recovering phenol from waste water containing phenol.
【０００２】[0002]
【従来の技術】フェノールは難分解性物質であり、微生
物による処理が困難である。フェノール樹脂製造工程か
ら排出されるフェノール含有排水は、メチルイソブチル
ケトン (ＭＩＢＫ) 等の抽出剤でフェノールを抽出、除
去した後に大量の水で希釈し、活性汚泥法で処理され、
放流されている。2. Description of the Related Art Phenol is a persistent substance and is difficult to treat with microorganisms. The phenol-containing wastewater discharged from the phenol resin manufacturing process is treated with an activated sludge method after extracting and removing phenol with an extractant such as methyl isobutyl ketone (MIBK) and diluting it with a large amount of water.
Has been released.
【０００３】抽出剤で抽出されたフェノールとＭＩＢＫ
との混合溶液からは蒸留によってフェノールが分離、回
収され、ＭＩＢＫはデカンタにおいて水と相分離され、
回収されている。しかしながら、かかる抽出剤を用いる
フェノールの分離、回収方法は、ＭＩＢＫによる抽出
塔、ＭＩＢＫとフェノール混合溶液の蒸留塔、ＭＩＢＫ
と水の相分離のためのデカンタなど多くの機器を必要と
すると共に、水資源、抽出剤およびエネルギーの浪費を
ともない、運転コストの増大を招くなどの問題点があっ
た。Phenol and MIBK extracted with an extractant
Phenol is separated and recovered from the mixed solution with and MIBK is phase-separated from water in the decanter,
Has been recovered. However, the method of separating and recovering phenol using such an extractant is as follows: extraction column by MIBK, distillation column of MIBK and phenol mixed solution, MIBK
There are problems that many devices such as a decanter for phase separation of water and water are required, and water resources, extractant and energy are wasted, and operating costs increase.
【０００４】[0004]
【発明が解決しようとする課題】本発明が解決せんとす
る課題は、抽出剤、希釈水を不要とし、かつ構成機器の
簡素化と運転コストの低廉化をはかることにある。The problem to be solved by the present invention is to eliminate the need for an extractant and diluting water, and to simplify the constituent equipment and reduce the operating cost.
【０００５】[0005]
【課題を解決するための手段】上記課題を解決するため
の本発明は、フェノール含有排水を減圧下で蒸発、凝縮
させ、次いで凝縮した排水を浸透気化膜を備えた分離装
置に供給して減圧側の透過液からフェノール−アルデヒ
ドを分離、回収することを特徴とするものである。以
下、本発明の原理を図１に示す原理図により説明する。According to the present invention for solving the above-mentioned problems, a phenol-containing wastewater is evaporated and condensed under reduced pressure, and then the condensed wastewater is supplied to a separator equipped with a pervaporation membrane to reduce the pressure. It is characterized by separating and recovering phenol-aldehyde from the permeate on the side. Hereinafter, the principle of the present invention will be described with reference to the principle diagram shown in FIG.
【０００６】フェノール樹脂製造工程からの排水は、製
造対象がノボラック法またはレゾール法であるかによっ
て排水成分が多少異なるものの、フェノール以外に未反
応物であるフェノールの２量体、３量体などの低分子量
ポリマーが含まれている。そこで本発明においては、ま
ず、フェノール樹脂製造工程からのフェノール含有排水
を減圧処理、たとえば減圧フラッシュ処理、すなわち減
圧下で蒸発、凝縮させ、残留する低分子量フェノール樹
脂や固形物を除去した排水を図１に示す浸透気化測定装
置で処理した。The wastewater from the phenol resin production process has a slightly different wastewater component depending on whether the production object is the novolac method or the resol method. However, in addition to phenol, unreacted phenol dimers, trimers, etc. Includes low molecular weight polymers. Therefore, in the present invention, first, the phenol-containing wastewater from the phenol resin production process is subjected to a reduced pressure treatment, for example, a reduced pressure flash treatment, that is, a wastewater obtained by evaporating and condensing under a reduced pressure and removing the residual low molecular weight phenolic resin and solid matter is illustrated. It processed with the pervaporation measuring apparatus shown in 1.
【０００７】浸透気化膜１はフランジベースのセル２に
セットされており、有効膜面積は22.04cm2 である。膜
１としては、有機物選択性能が非常に優れているシリコ
ーン系膜 (特開昭58-84005) 、ポリアセチレン系膜 (特
開昭61‐174905および特開平１-194903)、ポリアクリル
酸系膜およびポリエーテル系膜 (特開昭57-63101）など
が用いられる。膜面上のガラス容器３内に300ml の上記
減圧処理をした排水を供給し、マグネチックスターラ４
で攪拌する。この供給液は、ガラスヒーター５およびヒ
ーターコントローラ６で常に50℃に調整してある。The pervaporation membrane 1 is set in the flange-based cell 2, and the effective membrane area is 22.04 cm 2 . As the membrane 1, a silicone-based membrane (JP-A-58-84005), a polyacetylene-based membrane (JP-A-61-174905 and JP-A-1-194903) having excellent organic matter selection performance, a polyacrylic acid-based membrane and A polyether film (JP-A-57-63101) or the like is used. 300 ml of the depressurized wastewater was supplied into the glass container 3 on the membrane surface, and the magnetic stirrer 4
Stir with. This supply liquid is constantly adjusted to 50 ° C. by the glass heater 5 and the heater controller 6.
【０００８】膜１の下面の透過側の真空度は真空ポンプ
７、電磁弁８およびセンサー９により１Torrに保たれて
いる。膜１の透過液はクーラー10により−30℃に冷却さ
れたエチレングリコール11で凝固され、容器12および13
に集められる。なお14はエチレングリコール11の温度コ
ントローラである。透過液の組成は、ガスクロマトグラ
フまたは吸光光度計により測定する。上記装置により5.
75重量％のフェノール含有排水を200ppmフェノール含有
濃度に低減させるのに必要な所要時間および膜１の性能
を求めた結果を表１に示す。The degree of vacuum on the permeate side of the lower surface of the membrane 1 is kept at 1 Torr by the vacuum pump 7, the solenoid valve 8 and the sensor 9. The permeate of the membrane 1 is solidified with ethylene glycol 11 cooled to −30 ° C. by a cooler 10 and then put into containers 12 and 13
Collected in. Reference numeral 14 is a temperature controller for ethylene glycol 11. The composition of the permeated liquid is measured by a gas chromatograph or an absorptiometer. With the above device 5.
Table 1 shows the results of the time required to reduce the wastewater containing 75% by weight of phenol to 200 ppm and the performance of the membrane 1.
【０００９】 膜１の透過性能は単位面積、単位時間当りの全透過量
(kg/m2h)と分離係数αにより比較した。なお、分離係数
αは下記式により求めた。[0009] The permeation performance of Membrane 1 is the total permeation amount per unit area and unit time.
(kg / m 2 h) and the separation coefficient α were compared. The separation coefficient α was calculated by the following formula.
【００１０】 ただし、Fph, Fw はそれぞれ供給液中のフェノール濃度
(重量％) と水分濃度(重量％) を示し、Pph, Pw はそ
れぞれ透過液中のフェノール濃度 (重量％) と水分濃度
(重量％) を示す。[0010] However, Fph and Fw are the phenol concentrations in the feed solution.
(Wt%) and water concentration (wt%), Pph and Pw are the phenol concentration (wt%) and water concentration in the permeate, respectively.
(% By weight) is shown.
【００１１】表１から明らかなとおり、フェノール含有
排水を浸透気化膜を用いれば、供給液中のフェノール濃
度に依存するものの、効率的にフェノール回収および処
理が可能である。以下、本発明を下記実施例により具体
的に説明する。As is clear from Table 1, if the permeation vaporization membrane is used for the phenol-containing wastewater, the phenol recovery and treatment can be efficiently carried out although it depends on the phenol concentration in the feed liquid. Hereinafter, the present invention will be specifically described with reference to the following examples.
【００１２】[0012]
【実施例】図２に示す工程で、かつ図２に示す装置を用
いてフェノール含有排水の処理を行なった。すなわち、
フェノール５重量％、不揮発分１重量％を含む排水 (水
含有量94重量％) を１kg/hの供給量で供給槽21、ポンプ
22、熱交換器23から、管路24、管路25、ヒーター26およ
びポンプ27を経てフラッシュエバポレータ28に供給し
た。EXAMPLE Phenol-containing wastewater was treated in the process shown in FIG. 2 and using the apparatus shown in FIG. That is,
Wastewater containing 5 wt% phenol and 1 wt% non-volatile content (water content 94 wt%) at a supply rate of 1 kg / h, supply tank 21, pump
From the heat exchanger 23 and the heat exchanger 23, it was supplied to the flash evaporator 28 via the pipe 24, the pipe 25, the heater 26 and the pump 27.
【００１３】エバポレータ28にはヒートポンプ29が組合
わされており、自己蒸発、凝縮する構造である。すなわ
ち、排水の蒸発に必要な熱量と凝縮に必要な冷熱源をヒ
ートポンプの操作により確保することができる。また、
真空ポンプ33によってエパポレータ28の外管側を143、
フラッシュ面10の上側を50mlterに保持した。A heat pump 29 is combined with the evaporator 28 and has a structure of self-evaporating and condensing. That is, the heat quantity required for evaporation of waste water and the cold heat source necessary for condensation can be secured by operating the heat pump. Also,
The outer tube side of the evaporator 28 is 143 by the vacuum pump 33,
The upper side of the flash surface 10 was held at 50 mlter.
【００１４】エバポレータ28に供給された排水は、内管
31を通過する間に加熱され、蒸発し、蒸気はデミスター
30、ヒートポンプ29を経て内管31の外管側に供給され、
内管31側を通る排水との熱変換により凝縮する。一方、
フェノール含有排水中に含まれる低分子量ポリマーや固
形物などの蒸発残留物はエバポレータ28から管路42によ
り除去した。この除去物の量は、残渣0.02kg/h、フェノ
ール0.003kg/h、水分0.007kg/h、不揮発分0.01kg/hであ
った。なお、ヒータ26は、主として始動時にヒートポン
プ29によって熱の受供バランスが得られるまで用いられ
るものであり、以後は排水をエバポレータ28へ供給する
ための管路の一部としての機能にとどまるようになる。The drainage supplied to the evaporator 28 is the inner pipe.
It heats up and evaporates as it passes through 31 and the vapor becomes a demister.
30, is supplied to the outer pipe side of the inner pipe 31 via the heat pump 29,
Condensation occurs due to heat conversion with wastewater that passes through the inner pipe 31 side. on the other hand,
Evaporation residues such as low molecular weight polymers and solids contained in the phenol-containing waste water were removed from the evaporator 28 by a line 42. The amount of the removed substance was 0.02 kg / h of residue, 0.003 kg / h of phenol, 0.007 kg / h of water, and 0.01 kg / h of nonvolatile content. It should be noted that the heater 26 is mainly used at the time of start-up until the heat receiving balance of the heat is obtained by the heat pump 29, and thereafter, the heater 26 only functions as a part of the conduit for supplying the waste water to the evaporator 28. Become.
【００１５】凝縮した、減圧処理ずみの排水をエバポレ
ータ28の外管側から排出し、管路32、ポンプ33および冷
却器34を経て膜分離装置35に供給した。この膜分離装置
35への供給液組成は、供給量0.98kg/h、フェノール含有
量4.８重量％、水含有量95.2重量％であった。膜分離装
置35としては、浸透気化膜36を備え、有効膜面積１m2
のプレート＆フレーム型モジュールを用いた。The condensed, decompressed waste water was discharged from the outer pipe side of the evaporator 28, and was supplied to the membrane separation device 35 through the pipe 32, the pump 33 and the cooler 34. This membrane separator
The composition of the liquid feed to No. 35 was 0.98 kg / h, the phenol content was 4.8% by weight, and the water content was 95.2% by weight. The membrane separation device 35 is equipped with a pervaporation membrane 36 and has an effective membrane area of 1 m 2
The plate & frame type module of was used.
【００１６】また、浸透気化膜36の浸透側を真空ポンプ
37によって２Torrに保持した。浸透液を管路38、冷却器
39を経て、ポンプ40により受槽41に回収した。回収液の
組成は、回収量0.109kg/h 、フェノール含有量43重量
％、水含有量57重量％であり、減圧処理と浸透気化膜に
よる分離との組合せによって、フェノール含有量５重量
％の供給排水をフェノール含有量43重量％に濃縮するこ
とができた。この回収液からのフェノールの分離・回収
は減圧処理と浸透気化膜との組合せにより容易に行なう
ことができる。The permeation side of the pervaporation membrane 36 is a vacuum pump.
Hold at 2 Torr by 37. Pipe line 38, cooler
After 39, it was collected in the receiving tank 41 by the pump 40. The composition of the recovered liquid is 0.109 kg / h, the phenol content is 43% by weight, and the water content is 57% by weight. The combined supply of reduced pressure treatment and permeation vaporization membrane provides a phenol content of 5% by weight. The wastewater could be concentrated to a phenol content of 43% by weight. Separation / recovery of phenol from the recovered liquid can be easily performed by a combination of a reduced pressure treatment and a pervaporation membrane.
【００１７】一方、浸透気化膜36の非透過液を管路43を
経て熱交換器23に供給し、エバポレータ28に供給される
排水の熱付与により冷却した後に管路44から処理ずみ排
水として取出した。この排水量は0.871kg/h 、フェノー
ル含有量は100ppm、水含有量は99.99重量％であった。
管路44で取出した処理ずみ排水中のフェノールを、活性
汚泥処理、活性炭処理あるいは逆浸透法処理によって更
に除去した。On the other hand, the non-permeated liquid of the pervaporation membrane 36 is supplied to the heat exchanger 23 via the pipe 43, cooled by heat application to the waste water supplied to the evaporator 28, and then taken out from the pipe 44 as treated waste water. did. The amount of discharged water was 0.871 kg / h, the phenol content was 100 ppm, and the water content was 99.99% by weight.
Phenol in the treated wastewater taken out through the pipeline 44 was further removed by activated sludge treatment, activated carbon treatment or reverse osmosis treatment.
【００１８】図３は活性汚泥処理を示し、管路44、ポン
プ45によって処理ずみ排水を活性汚泥処理槽46に導き、
処理ずみ排水中のフェノール (100ppm) を活性汚泥によ
って除去し、フェノール含有量２ppm 以下とした後に管
路47から放流した。図４は活性炭処理を示し、管路44、
ポンプ45を介して処理ずみ排水を活性炭塔48に供給し、
フェノール含有量２ppm 以下の排水として管路49から放
流した。FIG. 3 shows the activated sludge treatment, in which the treated wastewater is guided to the activated sludge treatment tank 46 by the pipe line 44 and the pump 45,
Phenol (100 ppm) in the treated wastewater was removed by activated sludge, the phenol content was reduced to 2 ppm or less, and then discharged from the pipe 47. FIG. 4 shows the activated carbon treatment, the line 44,
The treated wastewater is supplied to the activated carbon tower 48 via the pump 45,
It was discharged from the pipeline 49 as waste water having a phenol content of 2 ppm or less.
【００１９】なお、活性炭に吸着されたフェノールは、
管路50から水蒸気を供給し、排出液を管路51を介して浸
透気化膜分離装置35 (図２) への供給液に混入し、フェ
ノールを回収した。図５は逆浸透法処理を示し、管路4
4、ポンプ45によって処理ずみ排水を逆浸透膜装置52に
供給し、フェノール含有量２ppm 以下の浸透液を管路53
により放流した。The phenol adsorbed on the activated carbon is
Water vapor was supplied from the pipe 50, and the discharge liquid was mixed with the supply liquid to the pervaporation membrane separator 35 (FIG. 2) via the pipe 51 to recover phenol. Fig. 5 shows the reverse osmosis process, and the pipeline 4
4. The treated waste water is supplied to the reverse osmosis membrane device 52 by the pump 45, and the osmotic liquid having a phenol content of 2 ppm or less is supplied to the pipe 53
Released by.
【００２０】一方、濃縮されたフェノール水溶液を管路
54を経て浸透気化膜分離装置35 (図２) への供給液に混
入した。On the other hand, the concentrated phenol aqueous solution is
It was mixed with the feed liquid to the pervaporation membrane separator 35 (FIG. 2) via 54.
【発明の効果】本発明によれば、減圧処理と浸透気化膜
による透過との組合せによって、フェノール含有量５重
量％の排水を43重量％のフェノール含有排水に濃縮する
ことができる。一方、本発明により処理された排水中の
フェノールは、この排水を更に活性汚泥処理、活性炭処
理または逆浸透法で処理することによって容易に含有量
２ppm 以下に低下させることができる。According to the present invention, wastewater having a phenol content of 5% by weight can be concentrated to 43% by weight of phenol-containing wastewater by a combination of a reduced pressure treatment and permeation through a pervaporation membrane. On the other hand, the content of phenol in the wastewater treated according to the present invention can be easily reduced to 2 ppm or less by further treating the wastewater with an activated sludge treatment, an activated carbon treatment or a reverse osmosis method.
【００２１】従って従来のように抽出剤や多量の希釈水
が不要になり、かつ減圧処理のためのエバポレータと浸
透気化膜モジュールのみを必要とするだけなので構成機
器の簡素化と運転コストの低減をはかることができる。Therefore, unlike the conventional case, an extractant and a large amount of dilution water are not required, and only an evaporator and a pervaporation membrane module for decompression treatment are required, which simplifies the components and reduces the operating cost. You can measure.
【図１】本発明の原理を示す原理図である。FIG. 1 is a principle diagram showing the principle of the present invention.
【図２】本発明の工程を示す工程図である。FIG. 2 is a process drawing showing a process of the present invention.
【図３】処理ずみの排水中のフェノール含有量を２ppm
以下にするための工程図である。[Figure 3] Phenol content in treated wastewater is 2ppm
It is process drawing for making it below.
【図４】処理ずみ排水中のフェノール含有量を２ppm 以
下にするための、他の工程図である。FIG. 4 is another process diagram for reducing the phenol content in the treated wastewater to 2 ppm or less.
【図５】処理ずみ排水中のフェノール含有量を２ppm 以
下にするための、更に他の工程図である。FIG. 5 is another process drawing for reducing the phenol content in the treated wastewater to 2 ppm or less.
１ 浸透気化膜 ７ 真空ポンプ 28 減圧処理装置 29 ヒートポン
プ 35 膜分離装置 36 浸透気化膜 37 真空ポンプ 39 冷却器1 Pervaporation membrane 7 Vacuum pump 28 Decompression treatment device 29 Heat pump 35 Membrane separation device 36 Pervaporation membrane 37 Vacuum pump 39 Cooler
───────────────────────────────────────────────────── フロントページの続き (72)発明者 佐藤 博彦 東京都中央区築地５丁目６番４号 三井造 船株式会社内 (72)発明者 金田 愛三 茨城県結城市大字鹿窪1772−１ 日立化成 工業株式会社南結城工場内 (72)発明者 山崎 一雄 茨城県結城市大字鹿窪1772−１ 日立化成 工業株式会社南結城工場内 (72)発明者 越沼 敦 茨城県結城市大字鹿窪1772−１ 日立化成 工業株式会社南結城工場内 ─────────────────────────────────────────────────── ─── Continued Front Page (72) Inventor Hirohiko Sato 5-6-4 Tsukiji, Chuo-ku, Tokyo Mitsui Engineering & Ships Co., Ltd. (72) Inventor Aizo Kanada 1772-1 Kagoku, Yuki-shi, Ibaraki Hitachi Chemical Industrial Co., Ltd. Minami-Yuki Plant (72) Inventor Kazuo Yamazaki 172-1 Kagoku, Yuki-shi, Ibaraki Hitachi Chemical Co., Ltd. Minami-Yuki Plant, Inc. Kogyo Minami Yuki Factory
Claims (1)
縮させ、次いで凝縮した排水を浸透気化膜を備えた分離
装置に供給して減圧側の透過液からフェノールを分離、
回収することを特徴とするフェノール含有排水の処理方
法。1. Phenol-containing waste water is evaporated and condensed under reduced pressure, and then the condensed waste water is supplied to a separator equipped with a pervaporation membrane to separate phenol from the permeate on the reduced pressure side,
A method for treating phenol-containing wastewater, characterized by recovering.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP08876993A JP3434848B2 (en) | 1993-04-15 | 1993-04-15 | Treatment method for phenol-containing wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP08876993A JP3434848B2 (en) | 1993-04-15 | 1993-04-15 | Treatment method for phenol-containing wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH06296831A true JPH06296831A (en) | 1994-10-25 |
| JP3434848B2 JP3434848B2 (en) | 2003-08-11 |
Family
ID=13952072
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
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| JP08876993A Expired - Fee Related JP3434848B2 (en) | 1993-04-15 | 1993-04-15 | Treatment method for phenol-containing wastewater |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2007086224A1 (en) * | 2006-01-27 | 2007-08-02 | Idemitsu Kosan Co., Ltd. | Method of treating phenol-containing water and treating apparatus |
| CN103922530A (en) * | 2014-04-25 | 2014-07-16 | 哈尔滨工业大学 | Circulating forward osmosis and pervaporation integrated water treatment method |
| WO2014115687A1 (en) | 2013-01-25 | 2014-07-31 | 住友ベークライト株式会社 | Pervaporation membrane and method for concentrating phenol |
| JP2014147882A (en) * | 2013-01-31 | 2014-08-21 | Sumitomo Bakelite Co Ltd | Method for concentrating phenol |
| WO2015030156A1 (en) * | 2013-08-30 | 2015-03-05 | 住友ベークライト株式会社 | Method for separating, concentrating and/or collecting phenol, and system for achieving said method |
| CN104787955A (en) * | 2015-04-17 | 2015-07-22 | 青岛科技大学 | Method for removing organic matters in phenolic wastewater |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109052826A (en) * | 2018-08-21 | 2018-12-21 | 重庆渝茁科技有限公司 | The method for the treatment of city waste water of high-efficiency environment friendly |
-
1993
- 1993-04-15 JP JP08876993A patent/JP3434848B2/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2007086224A1 (en) * | 2006-01-27 | 2007-08-02 | Idemitsu Kosan Co., Ltd. | Method of treating phenol-containing water and treating apparatus |
| JP2007196171A (en) * | 2006-01-27 | 2007-08-09 | Idemitsu Kosan Co Ltd | Method and equipment for treating phenol-containing water |
| EP1995218A1 (en) * | 2006-01-27 | 2008-11-26 | Idemitsu Kosan Co., Ltd. | Method of treating phenol-containing water and treating apparatus |
| EP1995218A4 (en) * | 2006-01-27 | 2012-01-11 | Idemitsu Kosan Co | Method of treating phenol-containing water and treating apparatus |
| KR101304294B1 (en) * | 2006-01-27 | 2013-09-11 | 이데미쓰 고산 가부시키가이샤 | Method of treating phenol-containing water and treating apparatus |
| WO2014115687A1 (en) | 2013-01-25 | 2014-07-31 | 住友ベークライト株式会社 | Pervaporation membrane and method for concentrating phenol |
| JP2014147882A (en) * | 2013-01-31 | 2014-08-21 | Sumitomo Bakelite Co Ltd | Method for concentrating phenol |
| WO2015030156A1 (en) * | 2013-08-30 | 2015-03-05 | 住友ベークライト株式会社 | Method for separating, concentrating and/or collecting phenol, and system for achieving said method |
| CN103922530A (en) * | 2014-04-25 | 2014-07-16 | 哈尔滨工业大学 | Circulating forward osmosis and pervaporation integrated water treatment method |
| CN104787955A (en) * | 2015-04-17 | 2015-07-22 | 青岛科技大学 | Method for removing organic matters in phenolic wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3434848B2 (en) | 2003-08-11 |
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