JPH0521039B2 - - Google Patents
Info
- Publication number
- JPH0521039B2 JPH0521039B2 JP60023079A JP2307985A JPH0521039B2 JP H0521039 B2 JPH0521039 B2 JP H0521039B2 JP 60023079 A JP60023079 A JP 60023079A JP 2307985 A JP2307985 A JP 2307985A JP H0521039 B2 JPH0521039 B2 JP H0521039B2
- Authority
- JP
- Japan
- Prior art keywords
- nitrification
- tank
- membrane separation
- denitrification
- liquid
- 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 - Lifetime
Links
- 239000012528 membrane Substances 0.000 claims description 26
- 238000000926 separation method Methods 0.000 claims description 26
- 239000003795 chemical substances by application Substances 0.000 claims description 23
- 239000002699 waste material Substances 0.000 claims description 23
- 239000010802 sludge Substances 0.000 claims description 10
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 9
- 238000004140 cleaning Methods 0.000 claims description 7
- 230000001546 nitrifying effect Effects 0.000 claims description 5
- 239000002351 wastewater Substances 0.000 claims description 5
- 238000004065 wastewater treatment Methods 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 2
- 239000012670 alkaline solution Substances 0.000 claims 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 30
- 239000007788 liquid Substances 0.000 description 25
- 239000003513 alkali Substances 0.000 description 15
- 238000000034 method Methods 0.000 description 14
- 235000011121 sodium hydroxide Nutrition 0.000 description 10
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 238000001223 reverse osmosis Methods 0.000 description 8
- 238000000108 ultra-filtration Methods 0.000 description 7
- 241000894006 Bacteria Species 0.000 description 5
- 238000005406 washing Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 239000010800 human waste Substances 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000852 hydrogen donor Substances 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Description
【発明の詳細な説明】
［産業上の利用分野］
本発明は窒素含有廃水の処理装置に係り、特に
生物学的硝化脱窒処理手段と該手段からの処理液
を固液分離する膜分離装置とを有する処理装置に
関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a nitrogen-containing wastewater treatment device, and more particularly to a biological nitrification-denitrification treatment means and a membrane separation device for solid-liquid separation of the treated liquid from the means. The present invention relates to a processing device having:
［従来の技術］
窒素含有廃水の生物学的硝化脱窒処理方法は公
知であり、３相汚泥処理方式、２相汚泥処理方
式、或いは単相汚泥処理方式などがある。[Prior Art] Biological nitrification and denitrification treatment methods for nitrogen-containing wastewater are known, and include a three-phase sludge treatment method, a two-phase sludge treatment method, and a single-phase sludge treatment method.
また、生物学的に硝化脱窒処理した液を膜分離
装置に導入して処理し、処理水の水質の向上或い
は系内汚泥濃度の維持などを図るよう構成した装
置も公知である。 Furthermore, a device is also known that is configured to introduce biologically nitrified and denitrified liquid into a membrane separation device for treatment, thereby improving the water quality of the treated water or maintaining the sludge concentration in the system.
生物学的硝化脱窒処理方式の構成は、要すれば
次の通りである。 The structure of the biological nitrification and denitrification treatment method is as follows.
処理プロセスは硝化工程と脱窒工程とを有す
る。 The treatment process includes a nitrification step and a denitrification step.
硝化工程では、アンモニア成分を亜硝酸菌に
よりNO2に、硝酸菌によりNO3に酸化する。 In the nitrification process, the ammonia component is oxidized to NO 2 by nitrite bacteria and to NO 3 by nitrate bacteria.
NO2、NO3は各種の脱窒菌により無酸素条
件下でN2ガスに還元される。また水素共与体
或いは脱窒菌の育成のためにメタノールが脱窒
工程に添加されることも多い。 NO 2 and NO 3 are reduced to N 2 gas by various denitrifying bacteria under anoxic conditions. Furthermore, methanol is often added to the denitrification process to foster hydrogen donor or denitrification bacteria.
［発明が解決しようとする問題点］
しかして、生物学的硝化脱窒処理手段に後続し
て膜分離装置を設置した場合、この膜分離装置は
所定の時期にその内部を洗浄しなければならな
い。この洗浄には、通常、苛性ソーダ等のアルカ
リ剤を用いているのであるが、従来、この洗浄廃
液（以後、廃アルカリ剤ということがある）が有
効に利用されていなかつた。[Problems to be Solved by the Invention] However, when a membrane separation device is installed following the biological nitrification and denitrification treatment means, the inside of this membrane separation device must be cleaned at a predetermined time. . This cleaning usually uses an alkaline agent such as caustic soda, but until now, this cleaning waste liquid (hereinafter sometimes referred to as waste alkali agent) has not been effectively utilized.
［問題点を解決するための手段］
本発明は、窒素含有廃水を生物学的に硝化脱窒
処理する手段と、該生物学的硝化脱窒処理手段か
らの生物処理汚泥混合液を膜分離処理する膜分離
装置とを有する窒素含有廃水の処理装置におい
て、前記生物処理汚泥を濃縮分離した膜分離装置
の洗浄にアルカリ剤を用いると共に、洗浄後の廃
アルカリ液の全量を生物学的硝化脱窒処理手段の
硝化手段に返送する系を設けるようにしたもので
ある。[Means for Solving the Problems] The present invention provides a means for biologically nitrifying and denitrifying nitrogen-containing wastewater, and a membrane separation method for biologically treated sludge mixture from the biologically nitrifying and denitrifying means. In a nitrogen-containing wastewater treatment device having a membrane separation device that concentrates and separates the biologically treated sludge, an alkaline agent is used to clean the membrane separation device that concentrates and separates the biologically treated sludge, and the entire amount of the waste alkali solution after cleaning is subjected to biological nitrification and denitrification. A system for returning the water to the nitrification means of the processing means is provided.
［作用］
生物学的硝化脱窒処理手段における硝化工程に
おいては、硝化反応の進行に伴つてアルカリ度が
消費され、被処理液のPHが低下してくる。そし
て、硝化工程のPHが低下すると、硝化菌の活性が
低下する。そこで、通常は硝化工程において苛性
ソーダ等のアルカリ剤を添加し、PHを一定以上に
保つようにしているのであるが、その分だけ廃水
処理の薬品コストが高いものとなつている。[Function] In the nitrification process in the biological nitrification and denitrification treatment means, alkalinity is consumed as the nitrification reaction progresses, and the PH of the liquid to be treated decreases. When the pH of the nitrification process decreases, the activity of nitrifying bacteria decreases. Therefore, an alkaline agent such as caustic soda is usually added during the nitrification process to maintain the pH above a certain level, but this increases the cost of chemicals for wastewater treatment.
本発明によれば、膜分離装置の洗浄廃液の全量
がこの硝化工程に添加されるアルカリ剤として利
用されるので、廃アルカリ剤の再利用と、添加用
アルカリ剤の低減という二つの効果が同時に奏さ
れるのである。 According to the present invention, the entire amount of the washing waste liquid from the membrane separation device is used as the alkaline agent added to this nitrification process, so the two effects of reusing the waste alkali agent and reducing the amount of added alkaline agent are achieved at the same time. It is played.
［実施例］ 以下図面を参照して実施例について説明する。[Example] Examples will be described below with reference to the drawings.
第１図の実施例においては、窒素含有廃水はま
ず脱窒槽１に供給され嫌気的な処理を受けた後、
配管２から硝化槽３に送られ硝化処理される。硝
化処理液の一部は配管４から脱窒槽１に戻され脱
窒処理され、生じたN2ガスは脱窒槽１から系外
に抜き出される。脱窒処理を受けた液は配管２か
ら硝化槽３に送られる。硝化槽３の液のうちその
他の部分は配管５から膜分離装置６に送られ、膜
分離処理され、透過液は配管７から処理水として
取り出される。この膜分離装置６は、前述の如
く、所定の時期に、その内部を苛性ソーダ等のア
ルカリ剤で洗浄される。 In the embodiment shown in FIG. 1, nitrogen-containing wastewater is first supplied to the denitrification tank 1 and subjected to anaerobic treatment.
It is sent from piping 2 to nitrification tank 3 and undergoes nitrification treatment. A portion of the nitrification treatment liquid is returned to the denitrification tank 1 through the pipe 4 and subjected to denitrification treatment, and the generated N 2 gas is extracted from the denitrification tank 1 to the outside of the system. The denitrified liquid is sent from piping 2 to nitrification tank 3. The remaining part of the liquid in the nitrification tank 3 is sent from a pipe 5 to a membrane separator 6 and subjected to membrane separation treatment, and the permeate is taken out from a pipe 7 as treated water. As described above, the inside of the membrane separator 6 is cleaned with an alkaline agent such as caustic soda at a predetermined time.
而して、硝化槽３には、この硝化槽３内の処理
液のPHを所定値以上に維持すために、アルカリ剤
添加用配管８が接続されており、かつ膜分離装置
６の洗浄廃液たる廃アルカリ剤を返送する配管９
が接続されている。廃アルカリ剤の返送により、
配管８からのアルカリ剤の添加量が節減されると
共に、膜分離装置６の洗浄廃液の再利用が可能と
なる。また、廃アルカリ剤の再利用が行われるの
で、この廃アルカリ剤の処理のための設備が不要
となる。 The nitrification tank 3 is connected to an alkali agent addition pipe 8 in order to maintain the pH of the treated liquid in the nitrification tank 3 above a predetermined value, and is connected to a pipe 8 for adding an alkali agent, and also to connect the cleaning waste liquid of the membrane separation device 6 to the nitrification tank 3. Piping 9 for returning barrel waste alkali agent
is connected. By returning the waste alkaline agent,
The amount of alkaline agent added from the pipe 8 can be reduced, and the cleaning waste liquid from the membrane separation device 6 can be reused. Furthermore, since the waste alkali agent is reused, equipment for processing the waste alkali agent is not required.
なお実施例装置を実際の装置として稼動させる
に際しては、廃アルカリ剤を返送する配管９にそ
れぞれ廃アルカリ剤の受入槽や、これを送り出す
ポンプなどを必要に応じ適宜設置する。 When the apparatus of the embodiment is operated as an actual apparatus, a receiving tank for the waste alkali agent, a pump for sending it out, etc. are installed as appropriate in each of the pipes 9 for returning the waste alkali agent.
第２図は、本発明をし尿の処理装置に適用した
例を示す系統図である。 FIG. 2 is a system diagram showing an example in which the present invention is applied to a human waste processing device.
第２図において、除渣し尿はまず配管１０で第
１脱窒槽１１に送られる。その後配管１２から硝
化槽１３に送られ、硝化処理を受ける。この硝化
槽１３には、この硝化槽内の液のPHを所定値以上
に保つために、アルカリ剤（苛性ソーダ）を供給
するための配管１４が接続されている。また、こ
の硝化槽１３には、空気吹込手段１５が設置され
ている。 In FIG. 2, the removed human waste is first sent to a first denitrification tank 11 via a pipe 10. Thereafter, it is sent to a nitrification tank 13 through a pipe 12 and undergoes nitrification treatment. A pipe 14 for supplying an alkaline agent (caustic soda) is connected to the nitrification tank 13 in order to maintain the pH of the liquid in the nitrification tank above a predetermined value. Further, air blowing means 15 is installed in this nitrification tank 13.
また、硝化槽１３には、配管１６が接続され、
硝化処理された液を第１脱窒槽１１に供給してい
る。この配管１６から第１脱窒槽１１に導入され
た液は、この第１脱窒槽１１内で脱窒処理され、
生じたN2ガスは配管１７から系外に排出される。
また処理液は配管１２から硝化槽１３に戻され
る。 Further, a pipe 16 is connected to the nitrification tank 13,
The nitrified liquid is supplied to the first denitrification tank 11. The liquid introduced into the first denitrification tank 11 from this pipe 16 is denitrified in this first denitrification tank 11,
The generated N 2 gas is discharged from the system through piping 17.
Further, the processing liquid is returned to the nitrification tank 13 from the pipe 12.
硝化槽１３の処理液の残部は、配管１８から第
２脱窒槽１９へ送られ、脱窒処理を受ける。２０
はメタノール供給管、２１は脱窒反応によつて生
じたN2ガスを抜き出すための配管である。 The remainder of the treated liquid in the nitrification tank 13 is sent from the pipe 18 to the second denitrification tank 19 and undergoes denitrification treatment. 20
2 is a methanol supply pipe, and 21 is a pipe for extracting N 2 gas generated by the denitrification reaction.
第２脱窒槽１９の処理液は、配管２２から再曝
気槽２３に送られ、残留する余分なメタノールを
取り除く。再曝気槽２３には、配管２４が接続さ
れており、槽内の液の一部を返送汚泥として第１
脱窒槽１１に返送し得るよう構成されている。 The treated liquid in the second denitrification tank 19 is sent from a pipe 22 to a re-aeration tank 23 to remove remaining excess methanol. A pipe 24 is connected to the reaeration tank 23, and a part of the liquid in the tank is returned to the first tank as sludge.
It is configured so that it can be returned to the denitrification tank 11.
再曝気槽２３内の液の残部は、配管２５によつ
て限外濾過装置２６に送られる。 The remainder of the liquid in the reaeration tank 23 is sent to an ultrafiltration device 26 via piping 25.
限外濾過装置２６の濃縮側の出口水は配管２７
によつて再曝気槽２３に返送され透過水は、配管
２８によつて逆浸透膜分離装置２９に送られる。
逆浸透膜分離装置２９の濃縮側の出口水は、配管
３０から取り出され焼却等適宜処理される。また
逆浸透分離処理液は、配管３１から処理水として
系外に取り出される。 The outlet water on the concentration side of the ultrafiltration device 26 is connected to the pipe 27
The permeated water is returned to the reaeration tank 23 by the refrigeration tank 23, and the permeated water is sent to the reverse osmosis membrane separation device 29 via the piping 28.
The exit water on the concentration side of the reverse osmosis membrane separation device 29 is taken out from the pipe 30 and is appropriately treated such as incineration. Further, the reverse osmosis separation treatment liquid is taken out of the system from the pipe 31 as treated water.
限外濾過装置２６及び逆浸透膜分離装置２９
は、前述の如く、所定の時期に、その内部を苛性
ソーダ等のアルカリ剤で洗浄される。そして、こ
れら限外濾過装置２６及び逆浸透膜分離装置２９
から、各々の洗浄廃液たる廃アルカリ液の全量を
硝化槽１３に返送するための配管３２，３３が設
けられている。 Ultrafiltration device 26 and reverse osmosis membrane separation device 29
As mentioned above, the inside of the container is cleaned with an alkaline agent such as caustic soda at a predetermined time. These ultrafiltration device 26 and reverse osmosis membrane separation device 29
From there, pipes 32 and 33 are provided for returning the entire amount of the waste alkali solution, which is the washing waste liquid, to the nitrification tank 13.
而して、第２図の装置において除渣し尿の受入
量を100m3／日として運転を行つたところ、硝化
槽１３内のPHを7.0に保つには苛性ソーダ（100
％）を１Kg／m3必要であつた。一方、限外濾過装
置２６及び逆浸透膜分離装置２９からは洗浄廃液
としてNaOH（100％）としてそれぞれ0.25Kg／m3
及び0.01Kg／m3排出されたので、その分だけ新規
に投入する苛性ソーダの薬品量を節減することが
できた。即ち、従来においては、配管１４から硝
化槽１３に苛性ソーダを１日当り100Kg投入して
いたのであるが、本実施例においては、このうち
の25.1Kg分は洗浄廃液のものを使用することがで
き、従つて苛性ソーダの消費量を約25％節減する
ことができた。 When the apparatus shown in Fig. 2 was operated with a receiving amount of 100 m 3 /day of removed human waste, it was found that caustic soda (100 m 3 /day) was required to maintain the pH in the nitrification tank 13 at 7.0.
%) was required at 1Kg/ m3 . On the other hand, the ultrafiltration device 26 and the reverse osmosis membrane separation device 29 each output 0.25 Kg/m 3 of NaOH (100%) as washing waste liquid.
and 0.01Kg/m 3 , so the amount of newly introduced caustic soda chemicals could be reduced by that amount. That is, in the past, 100 kg of caustic soda was injected into the nitrification tank 13 from the pipe 14 per day, but in this embodiment, 25.1 kg of this can be used as washing waste liquid. Therefore, the consumption of caustic soda could be reduced by approximately 25%.
なお、本発明において生物学的硝化脱窒手段は
硝化工程を有するものならば、どのようなもので
も良く、本実施例に限定されるものではない。ま
た、膜分離装置としては、限外濾過装置、逆浸透
膜分離装置の他、精密濾過装置など各種のものを
用い得る。また、し尿以外の各種の窒素含有廃水
をも処理できることは明らかである。 In the present invention, the biological nitrification and denitrification means may be of any type as long as it has a nitrification process, and is not limited to this embodiment. Further, as the membrane separation device, various devices such as an ultrafiltration device, a reverse osmosis membrane separation device, and a precision filtration device can be used. It is clear that various nitrogen-containing wastewaters other than human waste can also be treated.
［効果］
以上詳述した通り、本発明の装置は、膜分離装
置の洗浄廃液たる廃アルカリ液の全量を硝化工程
に返送して再利用するよう構成したものであるの
で、従来硝化工程に必要とされているアルカリ剤
の必要量が相当部分廃アルカリ剤で代用でき、処
理に要する薬品コストを著しく低減することがで
きる。また、膜分離装置の洗浄廃液を処理するた
めの装置も不要となるなど、実用上の効果も大き
い。[Effects] As detailed above, the device of the present invention is configured so that the entire amount of the waste alkali solution, which is the washing waste liquid of the membrane separation device, is returned to the nitrification process and reused. A considerable portion of the required amount of alkali agent can be replaced with waste alkali agent, and the cost of chemicals required for treatment can be significantly reduced. Furthermore, it also has great practical effects, such as eliminating the need for a device for treating cleaning waste fluid from the membrane separation device.
第１図および第２図は本発明の実施例装置の系
統図である。
１……脱窒槽、３……硝化槽、６……膜分離装
置、９，３２，３３……廃アルカリ剤返送用配
管、１１……第１脱窒槽、１３……硝化槽、１９
……第２脱窒槽、２６……限外濾過装置、２９…
…逆浸透膜分離装置。
1 and 2 are system diagrams of an embodiment of the present invention. 1... Denitrification tank, 3... Nitrification tank, 6... Membrane separation device, 9, 32, 33... Piping for returning waste alkali agent, 11... First denitrification tank, 13... Nitrification tank, 19
...Second denitrification tank, 26...Ultrafiltration device, 29...
...Reverse osmosis membrane separation equipment.
Claims (1)
手段と、該生物学的硝化脱窒処理手段からの生物
処理汚泥混合液を膜分離処理する膜分離装置とを
有する窒素含有廃水の処理装置において、前記生
物処理汚泥を濃縮分離した膜分離装置の洗浄にア
ルカリ剤を用いると共に、洗浄後の廃アルカリ液
の全量を前記生物学的硝化脱窒処理手段の硝化手
段に返送する系を設けたことを特徴とする窒素含
有廃水の処理装置。1. A nitrogen-containing wastewater treatment device comprising a means for biologically nitrifying and denitrifying nitrogen-containing wastewater and a membrane separation device for membrane-separating a biologically treated sludge mixture from the biologically nitrifying and denitrifying treatment means. In addition to using an alkaline agent to clean the membrane separation device that concentrated and separated the biologically treated sludge, a system was provided for returning the entire amount of the waste alkaline solution after cleaning to the nitrification means of the biological nitrification and denitrification treatment means. A nitrogen-containing wastewater treatment device characterized by:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60023079A JPS61181594A (en) | 1985-02-08 | 1985-02-08 | Treating device of waste water containing nitrogen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60023079A JPS61181594A (en) | 1985-02-08 | 1985-02-08 | Treating device of waste water containing nitrogen |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS61181594A JPS61181594A (en) | 1986-08-14 |
| JPH0521039B2 true JPH0521039B2 (en) | 1993-03-23 |
Family
ID=12100406
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60023079A Granted JPS61181594A (en) | 1985-02-08 | 1985-02-08 | Treating device of waste water containing nitrogen |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS61181594A (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63221893A (en) * | 1987-03-09 | 1988-09-14 | Ebara Infilco Co Ltd | Treatment of organic sewage |
| JPH02218500A (en) * | 1989-02-20 | 1990-08-31 | Ebara Infilco Co Ltd | Treatment of excretion type sewage |
| JPH02245296A (en) * | 1989-03-17 | 1990-10-01 | Ebara Infilco Co Ltd | Treatment of organic waste water |
| JPH0659477B2 (en) * | 1990-07-11 | 1994-08-10 | 日本碍子株式会社 | Method for treating wastewater containing calcium and nitrogen |
| NL2001974C (en) * | 2008-09-10 | 2010-03-15 | Ipstar B V | DEVICE FOR TREATMENT OF UREA-WATER, TOILET, STABLE AND METHOD. |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4931151A (en) * | 1972-07-20 | 1974-03-20 | ||
| JPS5075177A (en) * | 1973-11-07 | 1975-06-20 | ||
| JPS5226379A (en) * | 1975-08-25 | 1977-02-26 | Asahi Chem Ind Co Ltd | Method of washing ultrafiltration membranes |
| JPS5394444A (en) * | 1977-01-29 | 1978-08-18 | Sanki Eng Co Ltd | Method of treating waste water containing highly concentrated ammonia nitrogen |
| JPS53106387A (en) * | 1977-02-28 | 1978-09-16 | Toshiba Corp | Washing method for membrane separation apparatus |
| JPS5498046A (en) * | 1978-01-18 | 1979-08-02 | Mitsui Toatsu Chem Inc | Method of purifying waste water |
-
1985
- 1985-02-08 JP JP60023079A patent/JPS61181594A/en active Granted
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4931151A (en) * | 1972-07-20 | 1974-03-20 | ||
| JPS5075177A (en) * | 1973-11-07 | 1975-06-20 | ||
| JPS5226379A (en) * | 1975-08-25 | 1977-02-26 | Asahi Chem Ind Co Ltd | Method of washing ultrafiltration membranes |
| JPS5394444A (en) * | 1977-01-29 | 1978-08-18 | Sanki Eng Co Ltd | Method of treating waste water containing highly concentrated ammonia nitrogen |
| JPS53106387A (en) * | 1977-02-28 | 1978-09-16 | Toshiba Corp | Washing method for membrane separation apparatus |
| JPS5498046A (en) * | 1978-01-18 | 1979-08-02 | Mitsui Toatsu Chem Inc | Method of purifying waste water |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS61181594A (en) | 1986-08-14 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EXPY | Cancellation because of completion of term |