JPH0561992B2 - - Google Patents
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- Publication number
- JPH0561992B2 JPH0561992B2 JP60045259A JP4525985A JPH0561992B2 JP H0561992 B2 JPH0561992 B2 JP H0561992B2 JP 60045259 A JP60045259 A JP 60045259A JP 4525985 A JP4525985 A JP 4525985A JP H0561992 B2 JPH0561992 B2 JP H0561992B2
- Authority
- JP
- Japan
- Prior art keywords
- reverse osmosis
- osmosis membrane
- membrane
- amount
- 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.)
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Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Activated Sludge Processes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Sludge (AREA)
Description
【発明の詳細な説明】
［産業上の利用分野］
本発明は、し尿や、家庭用浄化槽などの浄化槽
から発生する浄化槽汚泥などのし尿系汚水（以下
単にし尿という）を処理するための装置に関す
る。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a device for treating human waste and human waste water (hereinafter simply referred to as human waste) such as septic tank sludge generated from a septic tank such as a domestic septic tank. .
［従来の技術］
従来のし尿処理においては、し尿を生物学的に
処理し、処理水を汚泥分離処理した後、消毒等を
施して排出している。[Prior Art] In conventional human waste treatment, human waste is biologically treated, treated water is subjected to sludge separation treatment, and then disinfected and the like before being discharged.
また、この生物処理液には比較的高濃度の塩類
及びCOD成分が含まれているので、生物処理液
を逆浸透処理して濃縮する方法も提案されてい
る。 Furthermore, since this biological treatment liquid contains relatively high concentrations of salts and COD components, a method has also been proposed in which the biological treatment liquid is concentrated by reverse osmosis treatment.
また、し尿処理液等の廃水には、有機酸とアン
モニアとが含まれているが、有機酸とアンモニア
とを含む液からこれらを除去するために、まずア
ルカリを添加してアンモニアストリツピング処理
すると共に有機酸をアルカリ塩又はアルカリ金属
塩とし、しかる後逆浸透処理することも考えられ
る。 In addition, wastewater such as human waste treatment liquid contains organic acids and ammonia, but in order to remove these from the liquid containing organic acids and ammonia, an alkali is first added and ammonia stripping is performed. In addition, it is also conceivable to convert the organic acid into an alkali salt or an alkali metal salt and then perform reverse osmosis treatment.
［発明が解決しようとする問題点］
しかしながら、上記公知の方法に採用されてい
る逆浸透膜装置においては、安定した処理が困難
であつた。[Problems to be Solved by the Invention] However, in the reverse osmosis membrane device employed in the above-mentioned known method, stable treatment has been difficult.
即ち、生物処理液からCOD成分を除去する装
置として逆浸透膜装置を設置した場合、COD成
分の除去率を高めるために高排除率逆浸透膜を採
用すると、食塩除去率も高いので濃縮液の浸透圧
が高くなり、高濃縮ができず膜透過液量が少なく
なつてしまう。 In other words, when a reverse osmosis membrane device is installed as a device to remove COD components from biological treatment liquid, if a high rejection rate reverse osmosis membrane is used to increase the removal rate of COD components, the removal rate of salt will also be high, so The osmotic pressure increases, making it impossible to achieve high concentration, and the amount of membrane permeate decreases.
また、逆浸透膜装置は、運転の経過と共に膜の
分離性能が低下する。このような対策として、膜
性能回復剤を用いる場合があるが、このような薬
剤を加えた場合には、処理コストが増加すると共
に、薬剤が処理液側にリークして処理水質が低下
する恐れもある。 In addition, the separation performance of the reverse osmosis membrane device deteriorates as the operation progresses. As a countermeasure against this problem, membrane performance recovery agents may be used, but adding such agents increases treatment costs and there is a risk that the chemicals may leak into the treated solution and deteriorate the quality of the treated water. There is also.
さらに、アルカリを添加してアンモニアストリ
ツピング処理及び有機酸の塩への転換を行なつた
後、逆浸透膜処理する方法では、十分な浸透水量
が確保できないという問題がある。 Furthermore, in the method of adding an alkali to perform ammonia stripping treatment and conversion of organic acid into a salt, followed by reverse osmosis membrane treatment, there is a problem that a sufficient amount of permeated water cannot be secured.
即ち、し尿にアルカリを添加してアンモニアス
トリツピング処理した液には、多量の有機酸が含
まれるので、逆浸透膜としては高排除率のものを
用いざるを得ず、そのため、浸透水量も少なくな
る。 In other words, since the liquid obtained by adding alkali to human waste and ammonia stripping contains a large amount of organic acids, a reverse osmosis membrane with a high rejection rate must be used, and as a result, the amount of permeated water is also reduced. It becomes less.
［問題点を解決するための手段］
本発明は、上記従来の問題点を解消し、生物処
理液を膜分離装置を用いて処理する際し、透過液
量を低下させることなく処理水質を向上させ得る
し尿汚水の処理方法を提供することを目的として
いる。[Means for Solving the Problems] The present invention solves the above conventional problems and improves the quality of treated water without reducing the amount of permeate when biological treatment liquid is treated using a membrane separation device. The purpose of the present invention is to provide a method for treating human waste and sewage that can be used to treat wastewater.
この目的を達成するために、本発明は、し尿系
汚水を生物処理し、次いで該生物処理液を限外濾
過膜で膜分離処理して得た透過水に酸を添加して
PHを4.8〜6.5に調整した後、食塩除去率の低い低
排除率逆浸透膜で膜分離処理するようにしたもの
である。 In order to achieve this objective, the present invention biologically treats human waste wastewater, then membrane-separates the biologically treated liquid using an ultrafiltration membrane, and adds an acid to the permeated water obtained.
After adjusting the pH to 4.8 to 6.5, membrane separation is performed using a low rejection rate reverse osmosis membrane that has a low salt removal rate.
以下本発明の構成についてさらに詳細に説明す
る。 The configuration of the present invention will be explained in more detail below.
本発明においては、し尿をまず生物処理する。
これによりし尿中のBOD成分や窒素成分が消化
ないしは脱窒され、し尿中の有機酸及びアンモニ
アも十分に低い濃度となる。そのため後段に設置
する逆浸透膜として除去率のそれ程高くないもの
が使用可能となり、透過水量を確保しつつ、高濃
縮を行うことができる様になる。 In the present invention, human waste is first subjected to biological treatment.
As a result, the BOD components and nitrogen components in the human urine are digested or denitrified, and the concentrations of organic acids and ammonia in the human urine are also reduced to sufficiently low levels. Therefore, it becomes possible to use a reverse osmosis membrane installed in the latter stage that does not have a very high removal rate, and it becomes possible to perform high concentration while ensuring the amount of permeated water.
この生物処理液は、次いで限外濾過膜分離処理
に供し、その透過水を逆浸透膜分離処理に供する
が、この逆浸透膜分離処理に先立つて、限外濾過
膜分離処理の透過水に酸を添加してPHを4.8〜6.5
に調整する。なお、し尿処理液のPHは、通常7.5
〜8.5程度である。 This biological treatment liquid is then subjected to ultrafiltration membrane separation treatment, and the permeated water is subjected to reverse osmosis membrane separation treatment. Add to adjust pH to 4.8-6.5
Adjust to. In addition, the pH of human waste treatment liquid is usually 7.5.
It is about ~8.5.
一般に、し尿生物処理液はCa2+イオン等の無
機スケール成分の含み、またPH８前後であるため
スケールが析出しやすい状態にある。この液を限
外濾過膜で処理した後、その透過水を逆浸透膜で
処理すると、逆浸透膜の膜面で部分的にスケール
成分が濃縮されるので、膜面にスケールが析出し
透過水量が低下する。 In general, human waste biological treatment liquid contains inorganic scale components such as Ca 2+ ions and has a pH of around 8, making it easy for scale to precipitate. When this liquid is treated with an ultrafiltration membrane and the permeated water is treated with a reverse osmosis membrane, scale components are partially concentrated on the membrane surface of the reverse osmosis membrane, so scale is precipitated on the membrane surface and the amount of permeated water increases. decreases.
これを防ぐためにはスケールが析出しないPH、
つまり酸性にして膜処理すれば良いが、被処理液
は、微生物代謝物質などの有機物質も含むので酸
性が強いとこれらの物質が凝集して逆に逆浸透膜
の目づまりの原因となる。 To prevent this, the pH must be set so that scale does not precipitate.
In other words, the membrane treatment can be carried out by making it acidic, but since the liquid to be treated also contains organic substances such as microbial metabolites, if the acidity is strong, these substances will aggregate and conversely cause clogging of the reverse osmosis membrane.
本発明においては、PHを4.8〜6.5に調整するこ
とにより、有機物質の凝集及びスケールの析出の
双方を抑制し、逆浸透膜の透過水量を十分に大き
くできる。 In the present invention, by adjusting the pH to 4.8 to 6.5, both aggregation of organic substances and precipitation of scale can be suppressed, and the amount of water permeated through the reverse osmosis membrane can be sufficiently increased.
なお、特に好ましいPHは4.9〜6.0である。 Note that a particularly preferable pH is 4.9 to 6.0.
本発明において、PH調整に使用する薬品は塩
酸、硫酸、炭酸など原液のPHを4.8〜6.5に調整で
きるものであれば何でも良いが、硝酸、リン酸は
窒素、リンを含むのであまり好ましくない。ま
た、硫酸、炭酸のような多塩基酸は逆浸透膜の除
去率が高いため濃縮されやすく、濃縮液の浸透圧
増加の一因となるのでコスト面等のメリツトがな
ければ使用は好ましくない。それ故、本発明にお
いて、PH調整には塩酸を使用するのが最も望まし
い。 In the present invention, any chemicals used for pH adjustment may be used as long as they can adjust the pH of the stock solution to 4.8 to 6.5, such as hydrochloric acid, sulfuric acid, and carbonic acid, but nitric acid and phosphoric acid are not so preferred because they contain nitrogen and phosphorus. Furthermore, polybasic acids such as sulfuric acid and carbonic acid have a high removal rate through reverse osmosis membranes, so they are easily concentrated and contribute to an increase in the osmotic pressure of the concentrated solution, so their use is not preferred unless there is an advantage in terms of cost or the like. Therefore, in the present invention, it is most desirable to use hydrochloric acid for pH adjustment.
なお、本発明においては、限外濾過膜の濃縮水
を生物処理系統に戻すのが好ましい。このように
することにより、生物処理工程からの活性汚泥の
流出を防ぎ、高度な生物処理が行えるようにな
る。また、逆浸透膜へ導入される生物処理液中の
SS濃度も低下し、それだけ逆浸透膜の目詰りが
抑制されるようになる。 In addition, in the present invention, it is preferable to return the concentrated water of the ultrafiltration membrane to the biological treatment system. By doing so, activated sludge can be prevented from flowing out from the biological treatment process, and advanced biological treatment can be performed. In addition, in the biological treatment liquid introduced into the reverse osmosis membrane,
The SS concentration also decreases, and clogging of the reverse osmosis membrane is suppressed accordingly.
PHが調整された限外濾過膜処理の透過水は、次
に逆浸透膜処理される。 The PH-adjusted ultrafiltration membrane-treated permeate is then subjected to reverse osmosis membrane treatment.
本発明において、逆浸透膜としてはどのような
膜も使用できる。なお、本発明者らの研究の結
果、合成高分子膜は酢酸セルロース膜と異なり荷
電を持つものが多く、処理液のPHによりイオンの
透過が促進、又は抑制され、酸性側でイオンの透
過が促進され濃縮液の浸透圧増加を防ぐ作用が奏
されることが認められた。 In the present invention, any membrane can be used as the reverse osmosis membrane. As a result of the research conducted by the present inventors, unlike cellulose acetate membranes, many synthetic polymer membranes are electrically charged, and ion permeation is promoted or suppressed depending on the pH of the treatment solution, and ion permeation is reduced on the acidic side. It was observed that the effect of promoting the osmotic pressure increase in the concentrate was exerted.
本発明においては、逆浸透膜として、塩除去率
が例えば10〜60％程度と低い、いわゆるルーズ逆
浸透膜を用いる。本発明においては、このような
ルーズ逆浸透膜を用いるため、低圧で高濃縮が図
れ、水質の優れた処理水を高い浸透水量のもとで
得ることができるようになる。 In the present invention, a so-called loose reverse osmosis membrane having a low salt removal rate of, for example, about 10 to 60% is used as the reverse osmosis membrane. In the present invention, since such a loose reverse osmosis membrane is used, high concentration can be achieved at low pressure, and treated water of excellent quality can be obtained with a high amount of permeated water.
また、ルーズ逆浸透膜はSO4 2-イオンのような
多価イオンの除去率がCl-イオンのような一価イ
オンより著しく高い場合があり、とくに合成分子
系ルーズ逆浸透膜では顕著である。したがつてル
ーズ逆浸透膜を用いる本発明では、上記PH調整剤
の影響が大きい。そのため、PH調整剤の種類を選
定することにより、濃縮液の浸透圧を調節するこ
とも可能である。 In addition, loose reverse osmosis membranes may have a significantly higher removal rate of multivalent ions such as SO 4 2- ions than monovalent ions such as Cl - ions, and this is especially noticeable with synthetic molecular loose reverse osmosis membranes. . Therefore, in the present invention using a loose reverse osmosis membrane, the influence of the above-mentioned PH adjuster is large. Therefore, by selecting the type of PH adjuster, it is also possible to adjust the osmotic pressure of the concentrate.
以下図面を参照して本発明をさらに説明する。 The present invention will be further described below with reference to the drawings.
第１図は本発明方法を実施するに好適な装置の
一例を示す系統図である。第１図において、スク
リーン等によつて夾雑物を除去された除渣し尿
は、生物処理手段１に送られ、BOD成分の分解
や窒素成分の硝化脱窒処理が施される。この処理
液は、配管２から限外濾過装置３へ送られる。限
外濾過装置３の限外濾過膜３ａを透過しない部分
は配管４から生物処理手段１に返送される。 FIG. 1 is a system diagram showing an example of an apparatus suitable for carrying out the method of the present invention. In FIG. 1, human waste from which impurities have been removed by a screen or the like is sent to a biological treatment means 1, where BOD components are decomposed and nitrogen components are nitrified and denitrified. This treatment liquid is sent from piping 2 to ultrafiltration device 3 . The portion of the ultrafiltration device 3 that does not pass through the ultrafiltration membrane 3a is returned to the biological treatment means 1 through the piping 4.
限外濾過膜３ａを透過した透過液は、配管５か
らルーズ逆浸透分離装置６に送られる。また、こ
の途中で配管９により酸が添加され、PH4.8〜6.5
好ましくは4.0〜6.0に調整される。 The permeated liquid that has passed through the ultrafiltration membrane 3a is sent from a pipe 5 to a loose reverse osmosis separation device 6. Also, during this process, acid is added through pipe 9, and the pH is 4.8 to 6.5.
Preferably it is adjusted to 4.0 to 6.0.
ルーズ逆浸膜分離装置６は、ルーズな逆浸透膜
６ａを備えているので、高濃縮することができ
る。濃縮液は配管７から取り出され、蒸発或いは
焼却等の工程に送られる。また、ルーズ逆浸透膜
６ａを透過した液は、配管８から処理水として取
り出され、放流工程や再利用工程に送られる。 Since the loose reverse osmosis membrane separator 6 includes a loose reverse osmosis membrane 6a, it can highly concentrate. The concentrated liquid is taken out from the pipe 7 and sent to a process such as evaporation or incineration. Further, the liquid that has passed through the loose reverse osmosis membrane 6a is taken out as treated water from the pipe 8 and sent to a discharge process or a reuse process.
前述のように、逆浸透膜６ａはルーズなもので
あるので、配管７から取り出される濃縮液の量は
少量であり、蒸発、焼却等の処理が容易である。
また、透過液も多量である。 As mentioned above, since the reverse osmosis membrane 6a is loose, the amount of concentrated liquid taken out from the pipe 7 is small, making it easy to process such as evaporation and incineration.
Also, the amount of permeate is large.
［作用］
本発明においては、し尿が生物処理された後、
限外濾過膜処理され、その透過水が逆浸透膜分離
処理されるので、逆浸透膜としては塩除去率の低
いルーズ逆浸透膜が用いられる。そのため、高濃
縮することができる。[Effect] In the present invention, after human waste is biologically treated,
Since the permeated water is subjected to an ultrafiltration membrane treatment and a reverse osmosis membrane separation treatment, a loose reverse osmosis membrane with a low salt removal rate is used as the reverse osmosis membrane. Therefore, it can be highly concentrated.
また、逆浸透膜処理するに際し、PHを4.8〜6.5
とすることにより、透過水量が著しく多量にな
る。 In addition, when performing reverse osmosis membrane treatment, the pH should be 4.8 to 6.5.
By doing so, the amount of permeated water becomes significantly large.
［実施例］
実施例 １
第１図に示す装置において、ルーズ逆浸透膜６
ａとして食塩除去率35％のものを用いた。[Example] Example 1 In the apparatus shown in FIG.
A sample with a salt removal rate of 35% was used as a sample.
そして、し尿を生物処理手段で処理した液を限
外濾過装置３に導入し、その透過液（CODMo360
mg／、電導率12000μs／cm）に塩酸を添加し、
PHを5.0に調整した後、ルーズ逆浸透膜分離装置
６に導入した。逆浸透処理の圧力は30Kg／cm2と
し、20倍濃縮した。このときの処理水のCODMo
は13.2mg／であり、平均透過水量は0.82m3／
m2／日であつた。また逆浸透膜の濃縮液の電導率
は41400μs／cm、透過液（処理水）の電導率は
11000μs／cmであつた。 Then, the liquid obtained by treating human waste with biological treatment means is introduced into the ultrafiltration device 3, and the permeated liquid (COD Mo 360
mg/, conductivity 12000μs/cm), and add hydrochloric acid to the
After adjusting the pH to 5.0, it was introduced into a loose reverse osmosis membrane separation device 6. The pressure of the reverse osmosis treatment was 30 Kg/cm 2 and the mixture was concentrated 20 times. COD Mo of treated water at this time
is 13.2 mg/, and the average permeate amount is 0.82 m 3 /
m 2 /day. In addition, the conductivity of the concentrated liquid of the reverse osmosis membrane is 41400μs/cm, and the conductivity of the permeate (treated water) is
It was 11000μs/cm.
実施例 ２
実施例１において、塩酸の代りに硫酸を用いた
他は同じ条件で処理を行つた。Example 2 The treatment was carried out under the same conditions as in Example 1 except that sulfuric acid was used instead of hydrochloric acid.
逆浸透膜の透過水量は0.82m3／m2／日、透過水
のCODMoは13.3ppmとほとんど同じであつた。 The amount of water permeated through the reverse osmosis membrane was 0.82 m 3 /m 2 /day, and the COD Mo of the permeated water was 13.3 ppm, which was almost the same.
また、濃縮液及び透過液の電動率は、それぞ
れ、51600μs／cm及び9770μs／cmであつた。 Further, the electric rates of the concentrated liquid and the permeated liquid were 51,600 μs/cm and 9,770 μs/cm, respectively.
比較例 １
実施例１において、塩酸の添加を行わなかつた
こと以外は同一条件で処理を行つた。その結果、
透過水量は著しく低下し、２倍濃縮しかできなか
つた。Comparative Example 1 The treatment was carried out under the same conditions as in Example 1 except that hydrochloric acid was not added. the result,
The amount of permeated water decreased significantly, and only 2-fold concentration was possible.
実施例３、比較例２
実施例１、比較例１において、濃縮倍率を変更
して透過水量を測定した。Example 3, Comparative Example 2 In Example 1 and Comparative Example 1, the amount of permeated water was measured while changing the concentration ratio.
その結果をその第２図に示す。 The results are shown in Figure 2.
第２図より、実施例によるものは高濃縮しても
高い透過水量を維持できることが明らかである。 From FIG. 2, it is clear that the sample according to the example can maintain a high amount of permeated water even when highly concentrated.
実施例４、比較例３
実施例１においてPHが４〜8.3の間の値となる
ように塩酸添加量を調節し、そのときの透過水量
を測定した。Example 4, Comparative Example 3 In Example 1, the amount of hydrochloric acid added was adjusted so that the pH was between 4 and 8.3, and the amount of permeated water at that time was measured.
その結果を第３図に示す。 The results are shown in FIG.
実施例５、比較例４
上記実施例４、比較例３において、濃縮倍率を
10倍とした他は、同一の条件として処理を行い、
透過水量を測定した。Example 5, Comparative Example 4 In the above Example 4 and Comparative Example 3, the concentration ratio was
Processing was carried out under the same conditions except that it was multiplied by 10 times,
The amount of permeated water was measured.
その結果を第４図に示す。 The results are shown in FIG.
なお、第３図及び第４図においては、透過水量
は濃縮初期における透過水量Jiに対する20倍又は
10倍濃縮時の透過水量J20又はJ10の比として示さ
れている。 In addition, in Figures 3 and 4, the amount of permeated water is 20 times the amount of permeated water Ji at the initial stage of concentration, or
It is shown as a ratio of the amount of permeated water J 20 or J 10 when concentrated 10 times.
第３図ないし第４図より次のことが認められ
る。 The following is recognized from Figures 3 and 4.
PHが4.8よりも小さくなると、また6.5よりも
大きくなると透過水量が急激に低下する。 When the pH becomes smaller than 4.8 or larger than 6.5, the amount of permeated water decreases rapidly.
PHが4.9〜6.0の間では、透過水量は特に多く
なる。 When the pH is between 4.9 and 6.0, the amount of permeated water becomes particularly large.
濃縮倍率が小さいときにはPHを調整すること
の作用はそれ程顕著ではないが、濃縮倍率が高
くなると、PH調整による効果が極めて大きくな
る。 When the concentration factor is small, the effect of adjusting the PH is not so significant, but as the concentration factor increases, the effect of adjusting the PH becomes extremely large.
なお、通常の処理においては、高濃縮して濃
縮液の量を少なくし、これにより焼却等の処理
コストを低減するようにし、濃縮倍率としては
10倍以上となるようにする。 In addition, in normal processing, the amount of concentrated liquid is reduced by highly concentrating, thereby reducing processing costs such as incineration, and the concentration ratio is
Make it 10 times or more.
そのため、通常の処理においてPHを4.8〜6.5
とりわけ4.9〜6.0に調整すると、透明透過水量
が著しく増大する。 Therefore, in normal processing, the pH should be 4.8 to 6.5.
In particular, when adjusted to 4.9 to 6.0, the amount of transparent permeated water increases significantly.
［効果］
以上記述した通り、本発明はし尿を生物処理し
た後、限外濾過膜処理し、その透過水をPHを調整
し、次いでルーズ逆浸透膜分離処理するようにし
たものであり、逆浸透膜の透過液量を多くするこ
とができる。また逆浸透膜としてルーズ逆浸透膜
が採用するため、濃縮液の浸透圧を防ぎつつ高濃
縮できるようになる。また、この場合、有機性
COD成分の透過量は、高除去率の逆浸透膜と同
じであるので処理水質も優れたものになる。[Effect] As described above, in the present invention, human waste is biologically treated, then treated with an ultrafiltration membrane, the permeated water is adjusted to pH, and then subjected to a loose reverse osmosis membrane separation treatment. It is possible to increase the amount of liquid permeated through the osmotic membrane. In addition, since a loose reverse osmosis membrane is used as the reverse osmosis membrane, it is possible to achieve high concentration while preventing the osmotic pressure of the concentrated liquid. Also, in this case, organic
The amount of permeation of COD components is the same as that of a reverse osmosis membrane with a high removal rate, so the quality of the treated water is also excellent.
第１図は本発明の方法を説明する系統図であ
る。また第２図、第３図及び第４図はそれぞれ実
施例における測定結果を示すグラフである。
１……生物処理手段、３……限外濾過装置、６
……ルーズ逆浸透膜分離装置。
FIG. 1 is a system diagram illustrating the method of the present invention. Moreover, FIG. 2, FIG. 3, and FIG. 4 are graphs showing measurement results in Examples, respectively. 1... Biological treatment means, 3... Ultrafiltration device, 6
...Loose reverse osmosis membrane separation equipment.
Claims (1)
液を限外濾過膜で膜分離処理して得た透過水に酸
を添加してPHを4.8〜6.5に調整した後、食塩除去
率の低い低排除率逆浸透膜で膜分離処理すること
を特徴とするし尿系汚水の処理方法。1. After biologically treating human waste wastewater and then membrane-separating the biologically treated liquid with an ultrafiltration membrane, adding acid to the obtained permeated water to adjust the pH to 4.8 to 6.5, A method for treating night soil wastewater characterized by membrane separation treatment using a low rejection rate reverse osmosis membrane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60045259A JPS61204081A (en) | 1985-03-07 | 1985-03-07 | How to treat human waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60045259A JPS61204081A (en) | 1985-03-07 | 1985-03-07 | How to treat human waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS61204081A JPS61204081A (en) | 1986-09-10 |
| JPH0561992B2 true JPH0561992B2 (en) | 1993-09-07 |
Family
ID=12714285
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60045259A Granted JPS61204081A (en) | 1985-03-07 | 1985-03-07 | How to treat human waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS61204081A (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0667519B2 (en) * | 1986-06-10 | 1994-08-31 | 清 青嶋 | Method of treating feces, urine, organic sludge, sewage, etc. |
| JP2002186835A (en) * | 2000-12-20 | 2002-07-02 | Japan Organo Co Ltd | Operation method for reverse osmosis membrane device |
| JP4536740B2 (en) * | 2007-02-01 | 2010-09-01 | 株式会社神鋼環境ソリューション | Treatment method and treatment equipment for treated water |
| JP4612078B2 (en) * | 2007-12-10 | 2011-01-12 | 株式会社神鋼環境ソリューション | Biological treatment method and biological treatment apparatus |
| JP5194783B2 (en) * | 2007-12-27 | 2013-05-08 | 栗田工業株式会社 | Biological treatment method and apparatus for water containing organic matter |
| CN104418472A (en) * | 2013-09-11 | 2015-03-18 | 三菱丽阳株式会社 | Treatment device and treatment method of wastewater containing organic matters |
| CN108911266A (en) * | 2018-08-23 | 2018-11-30 | 温州嘉伟环保科技有限公司 | A kind of device and method of reverse osmosis membrane processing high rigidity sewage |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS50155054A (en) * | 1974-06-03 | 1975-12-13 | ||
| JPS54124875A (en) * | 1978-03-23 | 1979-09-28 | Mitsui Toatsu Chem Inc | Concentrating solution |
| JPS55128000A (en) * | 1979-03-27 | 1980-10-03 | Nitto Electric Ind Co | Treating of broth |
| JPS5735989A (en) * | 1980-08-08 | 1982-02-26 | Unitika Ltd | Disposal of night soil |
-
1985
- 1985-03-07 JP JP60045259A patent/JPS61204081A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS61204081A (en) | 1986-09-10 |
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|---|---|---|---|
| LAPS | Cancellation because of no payment of annual fees |