JPH0418994A - Treatment of organic waste water - Google Patents
Treatment of organic waste waterInfo
- Publication number
- JPH0418994A JPH0418994A JP2124473A JP12447390A JPH0418994A JP H0418994 A JPH0418994 A JP H0418994A JP 2124473 A JP2124473 A JP 2124473A JP 12447390 A JP12447390 A JP 12447390A JP H0418994 A JPH0418994 A JP H0418994A
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- flocculation reaction
- reaction tank
- filtrate
- water
- 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.)
- Pending
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 55
- 239000010815 organic waste Substances 0.000 title 1
- 239000012528 membrane Substances 0.000 claims abstract description 63
- 238000006243 chemical reaction Methods 0.000 claims abstract description 50
- 239000000706 filtrate Substances 0.000 claims abstract description 37
- 238000005189 flocculation Methods 0.000 claims abstract description 32
- 230000016615 flocculation Effects 0.000 claims abstract description 32
- 239000002351 wastewater Substances 0.000 claims abstract description 14
- 230000018044 dehydration Effects 0.000 claims abstract description 6
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 6
- 238000000926 separation method Methods 0.000 claims description 30
- 238000000034 method Methods 0.000 claims description 24
- 238000005345 coagulation Methods 0.000 claims description 14
- 230000015271 coagulation Effects 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 7
- 230000001112 coagulating effect Effects 0.000 claims description 3
- 208000005156 Dehydration Diseases 0.000 claims 3
- 239000000701 coagulant Substances 0.000 claims 1
- 239000007787 solid Substances 0.000 claims 1
- 239000010802 sludge Substances 0.000 abstract description 25
- 229920000642 polymer Polymers 0.000 abstract description 18
- 230000004907 flux Effects 0.000 abstract description 10
- 238000001179 sorption measurement Methods 0.000 abstract description 3
- 230000003311 flocculating effect Effects 0.000 abstract description 2
- 230000015556 catabolic process Effects 0.000 abstract 1
- 238000006731 degradation reaction Methods 0.000 abstract 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 6
- 229920006317 cationic polymer Polymers 0.000 description 6
- 239000010800 human waste Substances 0.000 description 6
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 6
- 230000002776 aggregation Effects 0.000 description 4
- 238000004220 aggregation Methods 0.000 description 4
- 238000004065 wastewater treatment Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000008186 active pharmaceutical agent Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241000218691 Cupressaceae Species 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 229960004887 ferric hydroxide Drugs 0.000 description 1
- IEECXTSVVFWGSE-UHFFFAOYSA-M iron(3+);oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Fe+3] IEECXTSVVFWGSE-UHFFFAOYSA-M 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
Description
【発明の詳細な説明】
［産業上の利用分野］
本発明は有機性廃水の処理方法に係り、特に、有機性廃
水を膜分離装置を備える処理装置で、処理するにあたり
、高い透過水量（フラックス）にて効率的に処理するこ
とができる有機性廃水の処理方法に関する。Detailed Description of the Invention [Industrial Application Field] The present invention relates to a method for treating organic wastewater, and in particular, when treating organic wastewater with a treatment device equipped with a membrane separation device, a high amount of permeated water (flux ) relates to a method for treating organic wastewater that can be efficiently treated.
［従来の技術〕
従来、し尿等の有機性廃水の処理方法の一つとして、有
機性廃水を生物反応槽にて生物処理した後、処理液を第
１のＵＦ（限外濾過）原水糟を経て第１のＵＦ膜分離装
置に送給し、膜透過水を凝集反応槽にて凝集処理し、凝
集処理水を更に第２のＬＩＦ原水槽を経て第２のＯＦ膜
分離装置に送給して処理する方法が行なわれている。[Prior art] Conventionally, as one method for treating organic wastewater such as human waste, organic wastewater is subjected to biological treatment in a biological reaction tank, and then the treated liquid is passed through a first UF (ultrafiltration) raw water sieve. The water permeated through the membrane is then coagulated in a coagulation reaction tank, and the coagulated water is further sent to a second OF membrane separator via a second LIF raw water tank. A method of processing is being used.
このようなし尿等の有機性廃水の生物処理工程からは、
大量の余剰汚泥が排出される。従来、余剰汚泥の処理に
は、凝集反応槽にて塩化第二鉄とカチオンポリマーを添
加して凝集した後、脱水機により脱水する方式が採られ
ている。この場合、余剰汚泥の凝集を十分に行なうため
に、凝集反応槽には、通常、過剰量の凝集剤が添加され
ている。また、脱水濾液は生物反応槽に返送されている
。From this biological treatment process of organic wastewater such as human waste,
A large amount of surplus sludge is discharged. Conventionally, surplus sludge has been treated by adding ferric chloride and a cationic polymer in a coagulation reaction tank, coagulating the sludge, and then dewatering the sludge using a dehydrator. In this case, in order to sufficiently flocculate excess sludge, an excessive amount of flocculant is usually added to the flocculation reaction tank. In addition, the dehydrated filtrate is returned to the biological reaction tank.
［発明が解決しようとする課Ｕ］
前述の如く、凝集反応槽においては、過剰量の凝集剤を
添加しているため、脱水濾液中には、凝集に寄与しない
カチオンポリマーが多く含有されている。カチオンポリ
マーは生物処理に悪影響を及ぼすものであるため、この
ようなカチオンポリマーを多量に含む脱水濾液を生物反
応槽に返送することは好ましいことではない。[Problem U to be solved by the invention] As mentioned above, in the flocculation reaction tank, an excessive amount of flocculant is added, so the dehydrated filtrate contains a large amount of cationic polymer that does not contribute to flocculation. . Since cationic polymers have an adverse effect on biological treatment, it is not preferable to return a dehydrated filtrate containing a large amount of such cationic polymers to the biological reaction tank.
このため、脱水濾液を第１のＵＦ膜分離装置の後工程の
凝集反応槽や第２のＬＩＦ原水槽に返送して、含有され
るカチオンポリマーを凝集処理に寄与させることも考え
られる。しかしながら、この場合には次のような問題が
ある。For this reason, it is also conceivable to return the dehydrated filtrate to the aggregation reaction tank or the second LIF raw water tank in the post-process of the first UF membrane separation device, so that the cationic polymer contained therein can contribute to the aggregation treatment. However, in this case, there are the following problems.
即ち、凝集反応槽では、′ｓ１のＵＦ膜の透過水に塩化
第二鉄を過剰量添加して酸性凝集を行なっているため、
第２のＯＦ原水槽は勿論のこと、凝集反応槽では既に塩
化第二鉄により凝集は完了しており、なお、ポリマーと
凝集する物質は存在しない。このため、脱水濾液を凝集
反応槽や第２のＩＦ原水槽に返送した場合、濾液に含有
されて導入されたポリマーか未反応、未凝集のまま遊離
の状態で液中に存在するものとなる。この遊離のポリマ
ーは、後工程の第２のＬＪＦ膜分離装置においてＵＦ膜
面に吸着し、その透過水量を低減させる。That is, in the flocculation reaction tank, acidic flocculation is performed by adding an excessive amount of ferric chloride to the permeated water of the UF membrane 's1.
In the coagulation reaction tank as well as in the second OF raw water tank, coagulation has already been completed by ferric chloride, and there is no substance that coagulates with the polymer. Therefore, when the dehydrated filtrate is returned to the flocculation reaction tank or the second IF raw water tank, the polymer contained in the filtrate and introduced will remain in the liquid in a free state, unreacted and unagglomerated. . This free polymer is adsorbed on the UF membrane surface in the second LJF membrane separator in the subsequent step, reducing the amount of permeated water.
また、第１のＵＦＩＩＩＫ分離装置は第１のＵＦ原水糟
の水位の変動に応じて間欠運転を行なっている。このた
め、第１のＵＦ膜分離装置の透過水は凝集反応槽に連続
して送給されず、間欠的に送給される。一方、脱水濾液
は連続的に送給されるものとなることから、第１のＵＦ
膜分離装置の停止時、即ち、第１のＵＦ膜分葭装置の透
過水が導入されないときには、当然、凝集反応槽又は第
２のＬＩＦ原水槽中には遊離のポリマーの存在量が多く
なり、第２のＵＦ膜分離装置の透過水量を著しく低減さ
せる。Further, the first UFIIIK separator is operated intermittently in response to fluctuations in the water level of the first UF raw water slag. Therefore, the permeated water of the first UF membrane separation device is not continuously fed to the flocculation reaction tank, but is fed intermittently. On the other hand, since the dehydrated filtrate is continuously fed, the first UF
When the membrane separator is stopped, that is, when the permeated water of the first UF membrane separator is not introduced, the amount of free polymer naturally increases in the flocculation reaction tank or the second LIF raw water tank. The amount of permeated water in the second UF membrane separator is significantly reduced.
本発明は上記従来の問題点を解決し、余剰汚泥の凝集、
脱水濾液を廃水処理工程に返送することによる膜の透過
水量の低下を防止して、効率的な処理を行なうことを可
能とする有機性廃水の処理方法を提供することを目的と
する。The present invention solves the above-mentioned conventional problems by coagulating excess sludge,
An object of the present invention is to provide a method for treating organic wastewater that enables efficient treatment by preventing a decrease in the amount of permeated water through a membrane due to returning the dehydrated filtrate to a wastewater treatment process.
［課題を解決するための手段］
本発明の有機性廃水の処理方法は、生物反応槽と、該槽
からの液を固液分離する第１の膜分離装置と、′ｆＳ１
の膜分離装置の透過水を凝集処理する凝集反応槽と、凝
集処理水を更に膜分離する第２の膜分離装置と、前記第
１及び／又は第２の膜分離装置の濃縮水に凝集剤を添加
して脱水する脱水処理装置と、脱水処理装置の濾液を凝
集反応槽に導入する手段と、を備える処理装置で有機性
廃水を処理する方法であって、該脱水処理装置の濾液を
、第１の膜分離装置の透過水が凝集反応槽に導入される
ときにのみ凝集反応槽に導入することを特徴とする。[Means for Solving the Problems] The organic wastewater treatment method of the present invention includes a biological reaction tank, a first membrane separation device for solid-liquid separation of a liquid from the tank, and a 'fS1
a coagulation reaction tank that coagulates the permeated water of the membrane separator, a second membrane separator that further membrane-separates the coagulated water, and a flocculant in the concentrated water of the first and/or second membrane separator. A method for treating organic wastewater with a treatment device comprising: a dehydration device that dehydrates the water by adding water; and a means for introducing the filtrate of the dehydration device into a flocculation reaction tank, the method comprising: It is characterized in that the permeated water of the first membrane separator is introduced into the aggregation reaction tank only when it is introduced into the aggregation reaction tank.
以下に図面を参照して本発明の詳細な説明する。The present invention will be described in detail below with reference to the drawings.
第１図は本発明の一実施方法を示す系統図である。FIG. 1 is a system diagram showing one implementation method of the present invention.
図示の方法において、し尿等の有機性廃水は、まず、配
管１１より生物反応槽１に供給され、槽内で生物処理さ
れる。生物処理水は次いでポンプ１２を備える配管１３
、第１のＵＦ原水槽２、及びポンプ１４を備える配管１
５を経て第１のＵＦ膜分離装置３に供給され、膜分離処
理される。第１のＯＦ膜分離装置３の濃縮水は配管１６
より抜き出され、一部は配管１７より第１のＵＦ原水槽
２に返送され、残部は余剰汚泥として配管１８より汚泥
凝集反応槽７に送給される。一方、第１のＵＰ膜分履装
置３の透過水は配管１９より凝集反応槽４に送給され、
配管４１より塩化第二鉄（ＦｅＣＩＬ３）等の凝集剤を
添加されて凝集処理される。凝集処理水は、ポンプ２０
を備える配管２１、第２のＩＦ原水４！５及びポンプ２
２を備える配管２３を経て第２のＵＦ膜分離装置６に供
給され、膜分離処理される。第２のＵＦ膜分離装置６の
濃縮水は配管２４より抜き出され、一部は配管２５より
第２のＵＦ原水檜５に返送され、残部は余剰汚泥として
配管２６より汚泥凝集反応Ｗ！７に送給される。一方、
第２のＵＦ膜分離装置６の透過水は配管２７より、系外
に排出され、必要に応じて活性炭処理等に供される。In the illustrated method, organic wastewater such as human waste is first supplied to the biological reaction tank 1 through a pipe 11 and subjected to biological treatment within the tank. The biologically treated water is then transferred to a pipe 13 equipped with a pump 12.
, a first UF raw water tank 2, and a pipe 1 including a pump 14
5 and then supplied to the first UF membrane separation device 3 where it is subjected to membrane separation processing. The concentrated water of the first OF membrane separation device 3 is connected to the pipe 16
A portion is returned to the first UF raw water tank 2 through a pipe 17, and the remainder is sent as surplus sludge to a sludge flocculation reaction tank 7 through a pipe 18. On the other hand, the permeated water from the first UP membrane separation device 3 is sent to the flocculation reaction tank 4 from the piping 19.
A flocculant such as ferric chloride (FeCIL3) is added through the pipe 41 to perform flocculation treatment. The flocculated water is pumped to the pump 20.
piping 21, second IF raw water 4!5 and pump 2
2 is supplied to the second UF membrane separation device 6 and subjected to membrane separation treatment. Concentrated water from the second UF membrane separator 6 is extracted from the pipe 24, a part of which is returned to the second UF raw water cypress 5 through the pipe 25, and the remainder is passed through the pipe 26 as surplus sludge through the sludge flocculation reaction W! 7. on the other hand,
The permeated water from the second UF membrane separation device 6 is discharged from the system through a pipe 27, and is subjected to activated carbon treatment, etc., if necessary.
配管１８及び２６より汚泥凝集反応槽７に導入された余
剰汚泥は、カチオンポリマー（配管４２）やＦｅＣ１Ｌ
３ （配管４３）等の凝集剤が添加され、凝集処理され
る、凝集処理水は配管２８より脱水機８に送給される。Excess sludge introduced into the sludge flocculation reaction tank 7 through the pipes 18 and 26 is mixed with cationic polymer (pipe 42) and FeC1L.
3 (piping 43), etc., and the flocculating treated water is fed to the dehydrator 8 through the piping 28.
脱水機８にて脱水処理された脱水汚泥は配管２９より系
外に排出され、焼却処理等に供される。一方、脱水濾液
は配管３０より濾液貯槽９に送給される。The dehydrated sludge that has been dehydrated in the dehydrator 8 is discharged from the system through a pipe 29 and is subjected to incineration or the like. On the other hand, the dehydrated filtrate is fed to the filtrate storage tank 9 through the piping 30.
本発明においては、この濾液貯槽９内の脱水濾液は、第
１のＵＦ膜分離装置３の稼動時、即ち、第１のＵＦ膜分
超装置３から透過水が配管１９より凝集反応槽４に導入
されるときのみに、配管３１（又は３２）より凝集反応
槽４に返送する。In the present invention, the dehydrated filtrate in the filtrate storage tank 9 is transferred to the coagulation reaction tank 4 from the first UF membrane separation device 3 through the pipe 19 when the first UF membrane separation device 3 is in operation. Only when it is introduced, it is returned to the flocculation reaction tank 4 through the piping 31 (or 32).
なお、この場合、脱水濾液を配管３１より第１のＵＦ膜
分離装置３の透過水と共に凝集反応槽４に導入するとき
は、該槽４へのＦ ｅ Ｃ１１３の添加に特に制限はな
いが、配管３２より脱水濾液を第１のＵＦ膜分離装置３
の透過水とは別に凝集反応槽４に導入する場合には、配
管４１からの該槽４へのＦ ｅ Ｃ１１３の添加を、脱
水濾液の導入よりも後に行なうのが、より効果的である
。即ち、配管４１からのＦ ｅ ＣｆＬ３の添加も間欠
的に行ない、第１のＵＦ膜分離装置３の透過水及び脱水
濾液の導入後、Ｆ ｅ Ｃ１１３を添加し、該透過水が
脱水濾液と混合された後、ＦｅＣ１Ｌ３が添加されるよ
うにする。In this case, when the dehydrated filtrate is introduced from the pipe 31 into the flocculation reaction tank 4 together with the permeated water of the first UF membrane separation device 3, there is no particular restriction on the addition of Fe C113 to the tank 4; The dehydrated filtrate is transferred from the pipe 32 to the first UF membrane separation device 3
When introducing Fe C113 into the flocculation reaction tank 4 separately from the permeated water, it is more effective to add Fe C113 from the pipe 41 to the tank 4 after the introduction of the dehydrated filtrate. That is, addition of F e CfL3 from the pipe 41 is also performed intermittently, and after introducing the permeated water and dehydrated filtrate of the first UF membrane separation device 3, F e C113 is added, and the permeated water is mixed with the dehydrated filtrate. After that, FeC1L3 is added.
このような本発明の方法によれば、遊１ｍ！（未反応）
のポリマーを含有する脱水濾液は、常に、ポリマーと凝
集反応する物質を含有する第１のＵＦ膜分離装置３の透
過水と共に導入されるようになるため、凝集反応槽４内
にて速やかに凝集し、その殆どがフロック内に含有され
たものとなる。このため、後工程の第２のＵＦ膜分離装
置６に導入される液中には、遊ＩＩＩ（未反応）のポリ
マーが殆ど存在することはなく、ポリマーの膜への吸着
による第２のＵＦ膜分離装置６のフラックスの低下は防
止される。According to the method of the present invention, the play is 1m! (unreacted)
The dehydrated filtrate containing the polymer is always introduced together with the permeated water of the first UF membrane separator 3 that contains substances that coagulate with the polymer, so it is quickly coagulated in the coagulation reaction tank 4. However, most of it is contained within the floc. Therefore, there is almost no free III (unreacted) polymer in the liquid introduced into the second UF membrane separation device 6 in the subsequent process, and the second UF is generated by adsorption of the polymer to the membrane. A decrease in the flux of the membrane separator 6 is prevented.
なお、第１図に示す実施方法は、本発明の一実施例であ
って、本発明はその要旨を超えない限り、何ら図示の方
法に限定されるものではない。Note that the implementation method shown in FIG. 1 is an example of the present invention, and the present invention is not limited to the illustrated method in any way unless it exceeds the gist thereof.
例えば、第１、第２のＵＦ原水槽はなくても良いが、安
定処理のためには、これを設けるのが有利である。また
、膜についてもＵＦ膜に限らず、他の膜であっても良い
。For example, although the first and second UF raw water tanks may not be provided, it is advantageous to provide them for stable processing. Further, the membrane is not limited to the UF membrane, but may be other membranes.
［作用］
本発明の有機性廃水の処理方法によれば、余剰汚泥の凝
集、脱水濾液を第１の膜分離装置の透過水が凝集反応槽
に導入されるときにのみ、凝集反応槽に導入するため、
脱水濾液中に存在する遊離（未反応）のポリマーは、凝
集反応槽内で優先的に凝集反応に寄与し、はぼ完全に凝
集する。この結果、後工程の第２の膜分離装置にはｔｌ
ｌｌＩ（未反応）のポリマーは送給されることは殆どな
い。[Function] According to the organic wastewater treatment method of the present invention, surplus sludge is coagulated and the dewatered filtrate is introduced into the coagulation reaction tank only when the permeated water from the first membrane separation device is introduced into the coagulation reaction tank. In order to
The free (unreacted) polymer present in the dewatered filtrate preferentially contributes to the flocculation reaction in the flocculation reaction tank, and is almost completely flocculated. As a result, the second membrane separator in the post-process has tl
Almost no llI (unreacted) polymer is delivered.
このため、ポリマーの膜面への吸着に起因する第２の膜
分離装置のフラックスの低下は防止される。Therefore, a decrease in the flux of the second membrane separation device due to adsorption of the polymer onto the membrane surface is prevented.
なお、凝集反応槽において、塩化第二鉄が過剰量添加さ
れても、それ自身水酸化第二鉄となってフロック化する
ため、過剰の塩化第二鉄が第２の膜分離装置のフラック
スを低下させるおそれはない。In addition, even if an excessive amount of ferric chloride is added in the flocculation reaction tank, it will turn into ferric hydroxide and form flocs, so the excess ferric chloride will absorb the flux of the second membrane separation device. There is no risk of deterioration.
［実施例コ 以下に実施例を挙げて本発明をより具体的に説明する。[Example code] EXAMPLES The present invention will be explained in more detail with reference to Examples below.
実施例１
第１図に示す処理フローにて、し尿１００ｋＩｌＺ日の
処理を行なった。Example 1 Human waste was treated for 100 kIlZ days according to the treatment flow shown in FIG.
なお、系内の多槽の処理条件等は下記の通りである。The processing conditions for the multiple tanks in the system are as follows.
１工」Ｊζ１±
余剰汚泥乾物重量：５．５ｋｇ−ＤＳ／ｋｊ２ＭＬＳＳ
＋ ２３０００ｍｇ／ｊ２
汚泥発生量＋２３．９ｍ″／日
第１のＵＦ原水槽２
余剰汚泥乾物重量：２．０ｋｇ−ＤＳ／ｋｉｔＭＬＳＳ
： ２００００ｍｇ／ｕ
汚泥発生量＋１０ｒｎ”７日
系全体（゛ ５日稼動）
汚泥発生量：４７．４６ｒｎ’／日
汚泥濃度（ＭＬＳＳ）： ２２１２０ｍｇ／ｕ汚泥凝集
応ｓ７
ポリマー添加量＋ １５．７５ｋｇ／日（ＳＳに対して
１．５％）
ボリマーリ〜り量・約１０％
脱水機８
ＳＳ回収率：９８％
脱水汚泥含水率；８０％
脱水濾液量：４６．２ｍ”７日
以上の条件から、し尿１００ｋｊ２／日を処理した場合
、脱水機８で発生する脱水濾液量と脱水濾液中に含まれ
るポリマー量は、それぞれ４６ｒｎ’／日、３２ ｍ
ｇ ／ １２となる。1 construction”Jζ1± Excess sludge dry weight: 5.5kg-DS/kj2MLSS
+23000mg/j2 Sludge generation amount +23.9m''/day 1st UF raw water tank 2 Excess sludge dry weight: 2.0kg-DS/kitMLSS
: 20000mg/u sludge generation amount + 10rn'' 7 days entire system (5 days operation) Sludge generation amount: 47.46rn'/day Sludge concentration (MLSS): 22120mg/u sludge flocculation response s7 Polymer addition amount + 15.75kg/day (1.5% for SS) Volimary volume: approx. 10% Dehydrator 8 SS recovery rate: 98% Dehydrated sludge water content: 80% Dehydrated filtrate volume: 46.2 m" From conditions of 7 days or more, human waste When processing 100 kj2/day, the amount of dehydrated filtrate generated in the dehydrator 8 and the amount of polymer contained in the dehydrated filtrate are 46 rn'/day and 32 m
g/12.
この脱水濾液を一旦濾液貯檀に送り、本発明に従って、
第１のＵＰＩ分離装置３が稼動して透過水が凝集反応槽
４に導入されるときのみ、凝集反応槽４に導入して処理
を行なった。This dehydrated filtrate is once sent to a filtrate reservoir, and according to the present invention,
Only when the first UPI separator 3 was in operation and the permeated water was introduced into the flocculation reaction tank 4, the permeated water was introduced into the flocculation reaction tank 4 and treated.
その結果、第２のＵＦ膜分離装置（平膜型ＵＦ＠）６の
フラックスは第１表に示す通りであった。As a result, the flux of the second UF membrane separation device (flat membrane type UF@) 6 was as shown in Table 1.
一方、脱水濾液を第１のＬＩＦ膜分離装置３の運転にか
かわらず、常に凝集反応槽４に導入したこと以外は、同
様にして処理を行なった場合の第２のＵＦ膜分離装置６
のフラックスは第１表に示す通りであった。On the other hand, the second UF membrane separation device 6 was treated in the same manner except that the dehydrated filtrate was always introduced into the flocculation reaction tank 4 regardless of the operation of the first LIF membrane separation device 3.
The flux was as shown in Table 1.
第１表
第１表の結果より明らかなように、比較例方法では脱水
濾液中の３２ ｍ ｇ ／ Ｉｔのポリマーのうち数％
がＳＳに吸着凝集されず、未反応のまま遊離の状態で存
在しているため、第２のＵＦ膜分離装置６のフラックス
を低下させているが、本発明法によれば、このような遊
離のポリマーが低減され、第２のＵＦ膜分離装置６のフ
ラックスが向上する効果が得られた。As is clear from the results in Table 1, in the comparative example method, a few percent of the 32 mg/It of polymer in the dehydrated filtrate
is not adsorbed and aggregated by SS and exists in an unreacted, free state, reducing the flux of the second UF membrane separation device 6. However, according to the method of the present invention, such free The effect of reducing the amount of polymer and improving the flux of the second UF membrane separation device 6 was obtained.
［発明の効果］
以上詳述した通り５本発明の有機性廃水の処理方法によ
れば、し尿等の有機性廃水の処理にあたり、余剰汚泥の
凝集、脱水濾液を返送することによる膜のフラックス低
下を防止して、効率的な処理を行なうことが可能とされ
る。[Effects of the Invention] As detailed above, according to the method for treating organic wastewater of the present invention, when treating organic wastewater such as human waste, coagulation of excess sludge and reduction in membrane flux by returning the dewatered filtrate are achieved. It is possible to prevent this and perform efficient processing.
第１図は本発明の有機性廃水の処理方法の一実施方法を
示す系統図である。
１・・・生物反応槽、
２・・・第１のＯＦ原水槽、
３・・・第１のＵＦ膜分離装置、
４・・・凝集反応槽、
５・・・Ｎ２のＵＦ原水槽、
６・・・ｙｓ、２のＵＦ膜分離装置、
７・・・汚泥凝集反応種、
８・・・脱水機、 ９・・・濾液貯槽。FIG. 1 is a system diagram showing one implementation method of the organic wastewater treatment method of the present invention. 1... Biological reaction tank, 2... First OF raw water tank, 3... First UF membrane separation device, 4... Coagulation reaction tank, 5... N2 UF raw water tank, 6 ...ys, 2 UF membrane separation device, 7... Sludge coagulation reaction species, 8... Dehydrator, 9... Filtrate storage tank.
Claims (1)
の膜分離装置と、第１の膜分離装置の透過水を凝集処理
する凝集反応槽と、凝集処理水を更に膜分離する第２の
膜分離装置と、前記第１及び／又は第２の膜分離装置の
濃縮水に凝集剤を添加して脱水する脱水処理装置と、脱
水処理装置の濾液を凝集反応槽に導入する手段と、を備
える処理装置で有機性廃水を処理する方法であって、該
脱水処理装置の濾液を、第１の膜分離装置の透過水が凝
集反応槽に導入されるときにのみ凝集反応槽に導入する
ことを特徴とする有機性廃水の処理方法。(1) A biological reaction tank and a first stage that separates the liquid from the tank into solid and liquid.
a membrane separator, a coagulation reaction tank for coagulating the permeated water of the first membrane separator, a second membrane separator for further membrane-separating the coagulated water, and the first and/or second membrane. A method for treating organic wastewater with a treatment device comprising: a dehydration device that adds a coagulant to the concentrated water of the separation device to dehydrate it; and a means for introducing the filtrate of the dehydration device into a coagulation reaction tank, the method comprising: A method for treating organic wastewater, characterized in that the filtrate from the dehydration treatment device is introduced into the flocculation reaction tank only when the permeated water from the first membrane separation device is introduced into the flocculation reaction tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2124473A JPH0418994A (en) | 1990-05-15 | 1990-05-15 | Treatment of organic waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2124473A JPH0418994A (en) | 1990-05-15 | 1990-05-15 | Treatment of organic waste water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0418994A true JPH0418994A (en) | 1992-01-23 |
Family
ID=14886392
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2124473A Pending JPH0418994A (en) | 1990-05-15 | 1990-05-15 | Treatment of organic waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0418994A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5364534A (en) * | 1992-10-02 | 1994-11-15 | Lyonnaise Des Eaux - Dumez | Process and apparatus for treating waste liquids |
| JPH07256295A (en) * | 1994-03-22 | 1995-10-09 | Ngk Insulators Ltd | Treatment of sewage return water |
| CN108706686A (en) * | 2018-05-29 | 2018-10-26 | 苏州膜海分离技术有限公司 | Batch-type flocculation-hyperfiltration treatment technique of micro-polluted water |
-
1990
- 1990-05-15 JP JP2124473A patent/JPH0418994A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5364534A (en) * | 1992-10-02 | 1994-11-15 | Lyonnaise Des Eaux - Dumez | Process and apparatus for treating waste liquids |
| JPH07256295A (en) * | 1994-03-22 | 1995-10-09 | Ngk Insulators Ltd | Treatment of sewage return water |
| CN108706686A (en) * | 2018-05-29 | 2018-10-26 | 苏州膜海分离技术有限公司 | Batch-type flocculation-hyperfiltration treatment technique of micro-polluted water |
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