JPS61200813A - Membrane separation apparatus - Google Patents
Membrane separation apparatusInfo
- Publication number
- JPS61200813A JPS61200813A JP60040945A JP4094585A JPS61200813A JP S61200813 A JPS61200813 A JP S61200813A JP 60040945 A JP60040945 A JP 60040945A JP 4094585 A JP4094585 A JP 4094585A JP S61200813 A JPS61200813 A JP S61200813A
- Authority
- JP
- Japan
- Prior art keywords
- reverse osmosis
- osmosis membrane
- water
- membrane separation
- loose reverse
- 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
- 239000012528 membrane Substances 0.000 title claims abstract description 105
- 238000000926 separation method Methods 0.000 title claims abstract description 31
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 61
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 52
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 17
- 150000003839 salts Chemical class 0.000 claims description 7
- 238000000034 method Methods 0.000 abstract description 8
- 238000001704 evaporation Methods 0.000 abstract description 3
- 230000008020 evaporation Effects 0.000 abstract description 3
- 239000007788 liquid Substances 0.000 description 21
- 239000010800 human waste Substances 0.000 description 8
- 239000012466 permeate Substances 0.000 description 8
- 230000003204 osmotic effect Effects 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 5
- 229920001059 synthetic polymer Polymers 0.000 description 5
- 239000012141 concentrate Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 101100009643 Papaver somniferum CODM gene Proteins 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000004760 aramid Substances 0.000 description 1
- 229920003235 aromatic polyamide Polymers 0.000 description 1
- 229920002301 cellulose acetate Polymers 0.000 description 1
- 239000011247 coating layer Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
- B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/02—Elements in series
- B01D2317/022—Reject series
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/02—Elements in series
- B01D2317/025—Permeate series
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Nanotechnology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、多段に設置された膜を有し、高度な処理水質
を得ることが出来る膜分離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 membrane separation device having membranes installed in multiple stages and capable of obtaining high quality treated water.
廃水の高度な処理装置として、膜分離装置が周知である
。Membrane separation devices are well known as advanced wastewater treatment devices.
例えばし尿や浄化槽等から発生する汚泥などを処理した
生物処理液には、比較的高濃度の塩類や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
方法が公知である。For example, biological treatment liquids obtained by treating human waste and sludge generated from septic tanks contain relatively high concentrations of salts and COD components, so there is a known method for concentrating biological treatment liquids through reverse osmosis treatment. be.
また、膜を多段に備えて被処理水を高度に浄化処理する
様にした膜分離装置として、
■ 限外濾過膜、この限外濾過膜の透過水を処理する逆
浸透膜、及びこの道通過膜の濃縮液を処理する第２の逆
浸透膜を備えた装置。In addition, as a membrane separation device equipped with multiple membranes to highly purify the water to be treated, An apparatus equipped with a second reverse osmosis membrane that processes membrane concentrate.
■ 限外濾過膜と、この限外濾過膜の透過水又は濃縮水
を処理する限外濾過膜を備えた装置。(2) A device equipped with an ultrafiltration membrane and an ultrafiltration membrane that processes permeated water or concentrated water of the ultrafiltration membrane.
■ 被処理水を処理する逆浸透膜、及びこの逆浸透膜の
濃縮側の液を処理するルーズな逆浸透膜を備えた装置。■ Equipment equipped with a reverse osmosis membrane that processes the water to be treated and a loose reverse osmosis membrane that processes the liquid on the concentrated side of this reverse osmosis membrane.
■ 被処理水を処理する限外濾過膜又は精密濾過■りと
、この限外濾過膜又は精密濾過膜の濃縮側の液を処理す
るルーズ逆浸透膜を備えた装置。(2) A device equipped with an ultrafiltration membrane or precision filtration membrane for treating water to be treated, and a loose reverse osmosis membrane for treating the liquid on the concentrated side of the ultrafiltration membrane or precision filtration membrane.
などが公知である。etc. are publicly known.
しかしながら、上記公知の膜分離装置においては、安定
した膜分離処理が困難であった。However, in the above-mentioned known membrane separation apparatus, it is difficult to perform stable membrane separation processing.
例えば、し尿の生物処理液からＣＯＤ成分を除去する装
置として逆浸透膜装置を用いた場合、ＣＯＤ成分の除去
率を高めるために高除去率逆浸透膜を採用すると、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
きず膜透過水量が少なくなってしまう、即ち、し尿の生
物処理液は浸透圧が６ ｋ ｇ ／ ｃ ｍ”前後あり
、通常の逆浸透膜で仮に１０倍濃縮すると、濃縮液の浸
透圧は約６０ ｋ ｇ ／ ｃ ｒｎ”にも達するので
、通常の逆浸透膜で高濃縮することはできない。For example, when a reverse osmosis membrane device is used as a device to remove COD components from biological treatment liquid of human waste, if a high removal rate reverse osmosis membrane is used to increase the removal rate of COD components, the salt removal rate is also high, so it is concentrated. The osmotic pressure of the liquid becomes high, making it impossible to achieve high concentration and reducing the amount of water that permeates through the membrane. In other words, the biological treatment liquid for human waste has an osmotic pressure of around 6 kg/cm", and if a normal reverse osmosis membrane is used, When concentrated 10 times, the osmotic pressure of the concentrated solution reaches approximately 60 kg/crn'', so it cannot be highly concentrated using a normal reverse osmosis membrane.
一方、ルーズ逆浸透膜と称される塩除去率の低い逆浸透
膜を用いると、透過水側に塩類が透過してくるので、濃
縮液の浸透圧はあまり増加せず、高濃縮が可能であるが
、ＣＯＤ除去率も低いので、ｌＯ倍程度濃縮すると透過
液の水質が悪化するという問題がある。On the other hand, when a reverse osmosis membrane with a low salt removal rate called a loose reverse osmosis membrane is used, salts permeate to the permeate side, so the osmotic pressure of the concentrated solution does not increase much and high concentration is possible. However, since the COD removal rate is low, there is a problem that the water quality of the permeate deteriorates when concentrated by about 10 times.
更に、膜を多段に設置する様にした上記■〜■の装置に
おいては次の様な問題があった。Furthermore, the above-mentioned apparatuses (1) to (3) in which the membranes are installed in multiple stages have the following problems.
ｉｆ）の装置においては、高除去率の逆浸透膜を２段に
設置しているので浸透圧が極めて大きくなる。従って、
後段側の逆浸透膜からは透過水がほとんど取れない。In the device of (if), the osmotic pressure becomes extremely high because reverse osmosis membranes with high removal rates are installed in two stages. Therefore,
Almost no permeated water can be removed from the reverse osmosis membrane at the rear stage.
■の装置においては、限外濾過膜は、ＣＯＤ除去率が高
くないので、限外濾過膜を多段に設けても、処理水の水
質はあまり良くならない。In the device (2), the ultrafiltration membrane does not have a high COD removal rate, so even if the ultrafiltration membrane is provided in multiple stages, the quality of the treated water will not improve much.
（■の装置においては、例えばこの装置をし尿の高度処
理に採用した場合、処理液の浸透圧が高いので、１段目
の逆浸透膜の濃縮率が上がらない。(In the case of the device (■), for example, if this device is used for advanced treatment of human waste, the concentration rate of the first stage reverse osmosis membrane will not increase because the osmotic pressure of the treatment liquid is high.
又、透過水量を大きくするには相当に高い圧力をかける
必要がある。Furthermore, in order to increase the amount of permeated water, it is necessary to apply a considerably high pressure.
■の装置においては、この装置をし尿の高度処理に採用
した場合、被処理液の浸透圧が高いので、第１段目の膜
の濃縮液を更に一段目よりも除去率の高い第２段目の膜
で処理するのは著しく困難である。In the device (2), when this device is used for advanced treatment of human waste, the osmotic pressure of the liquid to be treated is high, so the concentrated liquid from the first stage membrane is further transferred to the second stage, which has a higher removal rate than the first stage. It is extremely difficult to treat with eye membranes.
本発明は、上記従来の問題点を解消し、廃水を成分＃装
置を用いて処理するに際し、透過水量を低下させること
なく処理水質を向上させ得る膜分離装置を提供すること
を目的としている。The present invention solves the above conventional problems and provides a membrane separation device that can improve the quality of treated water without reducing the amount of permeated water when wastewater is treated using a component # device.
この目的を達成する為に、本発明は、被処理水を膜分離
処理する第１のルーズ逆浸透膜と、該ルーズ逆浸透膜か
らの濃縮水を膜分離処理する第２のルーズ逆浸透膜とを
有するよう構成したものである。In order to achieve this object, the present invention includes a first loose reverse osmosis membrane that performs membrane separation treatment on water to be treated, and a second loose reverse osmosis membrane that membrane separation treates concentrated water from the loose reverse osmosis membrane. It is configured to have the following.
本発明においては、逆浸透膜装置が第一段目の膜として
ルーズ逆浸透膜を備えているので、生物処理液等の処理
水の高濃縮ができる。そして、このルーズ逆浸透膜の濃
縮水は、同様に高濃縮が可能な第２のルーズ逆浸透膜に
よって処理を施されるので、装置全体として、高濃縮が
可能で、しかも処理水量を多く得ることができるように
なる。In the present invention, since the reverse osmosis membrane device is equipped with a loose reverse osmosis membrane as the first stage membrane, it is possible to highly concentrate treated water such as biological treatment liquid. Then, the concentrated water of this loose reverse osmosis membrane is treated by a second loose reverse osmosis membrane that is also capable of high concentration, so the entire device can achieve high concentration and obtain a large amount of treated water. You will be able to do this.
更に、低圧運転が可能であるので、装置運転に要する電
力量も少なくて足りる。Furthermore, since low-pressure operation is possible, less electric power is required to operate the device.
以下図面を参照して実施例について説明する。 Examples will be described below with reference to the drawings.
第１図は本発明の実施例装置の系統図である。FIG. 1 is a system diagram of an embodiment of the present invention.
第１図において、スクリーン等によって夾雑物を除去さ
れた除渣し尿等は、生物処理手段ｌに送られ、ＢＯＤ成
分の分解や窒素成分の硝化脱窒処理が施こされる。この
処理液は配管２から限外濾過装置３に送られる。限外濾
過装置の膜３ａを透過しない液は配管４から生物処理手
段ｌに返送される。In FIG. 1, the filtered human waste from which impurities have been removed by a screen or the like is sent to a biological treatment means 1, where it is subjected to decomposition of BOD components and nitrification and denitrification of nitrogen components. This treatment liquid is sent from piping 2 to ultrafiltration device 3 . The liquid that does not pass through the membrane 3a of the ultrafiltration device is returned to the biological treatment means l through the pipe 4.
限外濾過膜３ａの透過水は、配管５から第１のルーズ逆
浸透膜分離装置６に送られる。この第１のルーズ逆浸透
膜分離装置６は、第１のルーズ逆。The permeated water of the ultrafiltration membrane 3a is sent from the piping 5 to the first loose reverse osmosis membrane separation device 6. This first loose reverse osmosis membrane separation device 6 is a first loose reverse osmosis membrane separation device 6.
浸透膜６ａを備えており、被処理水を高濃縮することが
できる。透過液は配管７から取り出され、放流或いは再
利用等の工程に送られる。又、第１のルーズ逆浸透膜６
ａの濃縮液は、配管８から第２のルーズ逆浸透膜分離装
置９に送られる。この第２のルーズ逆浸透膜装置装Ｎ９
は第２のルーズ逆浸透膜９ａを備えており、被処理水を
高濃縮処理することができる。第２のルーズ逆浸透膜９
ａを透過した液は、配管ｌＯから配管５に戻され、第１
のルーズ逆浸透膜分離装置６に導入可能とされている。Equipped with a permeable membrane 6a, it is possible to highly concentrate the water to be treated. The permeate is taken out from the pipe 7 and sent to a process such as discharge or reuse. Moreover, the first loose reverse osmosis membrane 6
The concentrated liquid a is sent from a pipe 8 to a second loose reverse osmosis membrane separation device 9. This second loose reverse osmosis membrane device N9
is equipped with a second loose reverse osmosis membrane 9a, and can highly concentrate the water to be treated. Second loose reverse osmosis membrane 9
The liquid that has passed through a is returned to the pipe 5 from the pipe IO, and
It is said that it can be introduced into a loose reverse osmosis membrane separation device 6.
なお、逆浸透膜分離装置９において生じた濃縮液は、配
管１１によって取り出され、蒸発、燃焼等の処理工程へ
送られる。Note that the concentrated liquid produced in the reverse osmosis membrane separation device 9 is taken out through a pipe 11 and sent to processing steps such as evaporation and combustion.
＠述の様に、ルーズ逆浸透膜６ａ、９ａは塩除去率が低
いものであるので、配’Ｉｌｌ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。As mentioned above, since the loose reverse osmosis membranes 6a and 9a have a low salt removal rate, the amount of concentrated liquid taken out from the membrane is small, and processing such as evaporation and incineration is easy.
又、このルーズ逆浸透膜６ａ、９ａの透過水も多量であ
る。（なお、本発明者らの研究によれば、このルーズ逆
浸透膜６ａ、９ａの表面に、生物処理液中に含まれる高
分子成分のうち、限外濾過膜を透過した成分が耐着して
コーティング層を形成し、このコーティング層の作用に
よってルーズ逆透過膜６ａ、９ａの透過水のＣＯＤ濃度
が著しく低いものとなることが見出された。）
本実施例においては、第２のルーズ逆浸透膜９ａの透過
水を第１のルーズ逆浸透膜６ａの給液側に戻すようにし
ているので、この第１のルーズ逆浸透膜６ａへ導入され
る被処理液の被除去物質濃度が小さくなり、配管７から
取り出される処理水の水質が優れたものになる。勿論、
第２のルーズ逆浸透Ｉｌ＊９ａの透過水も、処理水とし
てそのまま系外に取り出しても良い。Also, a large amount of water permeates through the loose reverse osmosis membranes 6a and 9a. (According to the research conducted by the present inventors, components of the polymer components contained in the biological treatment liquid that have passed through the ultrafiltration membranes do not adhere to the surfaces of the loose reverse osmosis membranes 6a and 9a. (It was found that the COD concentration of the permeated water of the loose reverse permeation membranes 6a and 9a becomes extremely low due to the action of this coating layer.) In this example, the second loose Since the permeated water of the reverse osmosis membrane 9a is returned to the liquid supply side of the first loose reverse osmosis membrane 6a, the concentration of the substance to be removed in the liquid to be treated introduced into the first loose reverse osmosis membrane 6a is reduced. The water quality of the treated water taken out from the pipe 7 is excellent. Of course,
The permeated water of the second loose reverse osmosis Il*9a may also be taken out of the system as it is as treated water.
本発明において用いられるルーズ逆浸透膜としては、食
塩除去率が１０〜６０％、ＣＯＤ除去除去率９貝
しては、セルロースアセテートを主材とするものと、芳
香族ポリアミドなどを主材とする合成高分子系のものと
があり、本発明においてはいずれのものも用い得るので
あるが、耐薬品性に優れているところから合成高分子系
のものが望ましい。The loose reverse osmosis membranes used in the present invention have a salt removal rate of 10 to 60% and a COD removal rate of 9. The loose reverse osmosis membranes used in the present invention include those whose main material is cellulose acetate and those whose main material is aromatic polyamide. There are synthetic polymer-based ones, and any of them can be used in the present invention, but synthetic polymer-based ones are preferable because they have excellent chemical resistance.
なお、上記の説明では、主として被処理水がし尿又はし
尿系汚水である場合について説明したが１本発明はルー
ズ逆浸透膜で濃縮処理し得るその他の各種の廃水や用水
の処理に適用し得る。Although the above explanation mainly deals with cases where the water to be treated is human waste or human waste-based wastewater, the present invention can be applied to the treatment of various other types of wastewater and commercial water that can be concentrated using a loose reverse osmosis membrane. .
実験例
（本発明例）
第１図に示す装置において、ルーズ逆浸透膜６ａ、９ａ
としてＮａＣ１除去率５０％の合成高分子膜を用いた。Experimental example (example of the present invention) In the apparatus shown in FIG.
A synthetic polymer membrane with a NaCl removal rate of 50% was used.
限外濾過膜３ａを透過した水（電導率１１５０４ Ｓ
／ Ｃ ｍ 、Ｃ Ｏ Ｄ ｋ ３ ６ ０ Ｐ Ｐ
ｍ ）を第１のルーズ逆浸透膜分離装置６に導入し，圧
力３０ｋｇ／Ｃｍ″の条件で４倍濃縮した．この時の平
均透過水量は０ 、 ９ ８ｒｎ’／ｌｎ’／日であっ
た．このルーズ逆浸透膜分離装置６の濃縮液を、第２の
ルーズ逆浸透膜分離装置９に供給し、圧力３０ｋ ｇ
／ ｃ ｍ″の条件で５倍濃縮した．この時の平均透過
水量は０．６８ｍ”／ｍ″／日であった。Water that has passed through the ultrafiltration membrane 3a (electrical conductivity 11504 S
/ C m , C O D k 3 6 0 P P
m) was introduced into the first loose reverse osmosis membrane separation device 6 and concentrated 4 times under the condition of a pressure of 30 kg/Cm''.The average amount of permeated water at this time was 0.98rn'/ln'/day. .The concentrated liquid from the loose reverse osmosis membrane separation device 6 is supplied to the second loose reverse osmosis membrane separation device 9, and the pressure is 30 kg.
It was concentrated 5 times under the conditions of /cm''/cm''.The average amount of permeated water at this time was 0.68 m''/m''/day.
配管７から取り出される処理水は、電導率が８ ５ ６
０ ｐｓ／ｃｍ，ＣＯＤＭＩＩが１０ｐｐｍであった
。The treated water taken out from the pipe 7 has an electrical conductivity of 8 5 6
0 ps/cm, CODM II was 10 ppm.
（比較例１）
限外濾過膜の透過水（電導率１２０００井Ｓ／ｃｍ，Ｃ
０Ｉ）ｔａ３ ６ ０ ｐ ｐｍ）を、ＮａＣＪｌ除去
率９９．５％の合成高分子膜で、圧力５６ｋｇ／Ｃｍｌ
の条件で２．９倍に濃縮した．この時の平均透過水量は
１ 、 ３ｒｎ′／ｒｒｆ／日であった．実用的な透過
水量は、４倍以上の濃縮では得られなかった．なお、処
理水の水質は．電導率が１０５ＪＬｓ／ｃｍ，ＣＯＤＭ
ｊが０．２ｐｐｍであった。(Comparative Example 1) Permeated water of ultrafiltration membrane (electrical conductivity 12000 well S/cm, C
0I) ta3 60 p pm) using a synthetic polymer membrane with a NaCJl removal rate of 99.5% at a pressure of 56 kg/Cml.
It was concentrated 2.9 times under these conditions. The average amount of permeated water at this time was 1.3rn'/rrf/day. A practical amount of permeate water could not be obtained by concentrating 4 times or more. The quality of the treated water is. Electrical conductivity is 105JLs/cm, CODM
j was 0.2 ppm.
（比較例２）
比較例１と同じ限外濾過膜の透過水をＮａＣ文除去率５
０％の合成高分子系のルーズ逆浸透膜で圧力３０ｋｇ／
ｃｒｎ’の条件で２０倍濃縮した．この時の平均透過水
量は０ 、 ４ ２ｒｎ”７ｍ”７日であった．また、
処理水水質は、電導率が９７００ｇ５／ｃｍ，Ｃ０ＤＮ
１１が１３９Ｐｍであった。(Comparative Example 2) The NaC removal rate of the permeated water of the same ultrafiltration membrane as Comparative Example 1 was 5.
0% synthetic polymer loose reverse osmosis membrane with a pressure of 30 kg/
It was concentrated 20 times under crn' conditions. The average amount of permeated water at this time was 0.42rn"7m" for 7 days. Also,
The quality of the treated water has an electrical conductivity of 9700g5/cm, C0DN.
11 was 139 Pm.
上記の本発明例及び比較例１，２を比べると。Comparing the above-mentioned examples of the present invention and comparative examples 1 and 2.
本発明例においては、低い圧力で高濃縮することができ
、処理水水量も多いことが認められる．また、ルーズ逆
浸透膜の１段処理を行なっている比較例２に比べると、
処理水の水質も本発明例のものが優れていることが認め
られる。In the example of the present invention, it is recognized that high concentration can be achieved at low pressure and the amount of treated water is large. Also, compared to Comparative Example 2 in which one-stage treatment was performed using a loose reverse osmosis membrane,
It is recognized that the quality of the treated water is also excellent in the examples of the present invention.
以上詳述した通り、本発明はルーズ逆浸透膜を２段に備
えるよう構成したものであり、低い圧ヵで高濃縮でき、
かつ透過液量も多い。また、装置の運転電力コストも低
減できる。As detailed above, the present invention is configured to include two stages of loose reverse osmosis membranes, and can be highly concentrated at low pressure.
Also, the amount of permeate is large. Moreover, the operating power cost of the device can also be reduced.
第１図は本発明の実施例装置の系統図である。
１・・・生物処理手段。
３・・・限外濾過装置。
６・・・第１のルーズ逆浸透膜分離装置、９・・・第２
のルーズ逆浸透膜分離装置。FIG. 1 is a system diagram of an embodiment of the present invention. 1...Biological treatment means. 3...Ultrafiltration device. 6...First loose reverse osmosis membrane separation device, 9...Second
loose reverse osmosis membrane separation equipment.
Claims (3)
と、該ルーズ逆浸透膜の濃縮水を膜分離処理する第２の
ルーズ逆浸透膜とを有することを特徴とする膜分離装置
。(1) Membrane separation characterized by having a first loose reverse osmosis membrane that performs membrane separation treatment on water to be treated, and a second loose reverse osmosis membrane that performs membrane separation treatment on concentrated water of the loose reverse osmosis membrane. Device.
理水は、限外濾過膜の透過水であることを特徴とする膜
分離装置。(2) A membrane separation device according to claim 1, wherein the water to be treated is water permeated through an ultrafiltration membrane.
おいて、第１及び第２のルーズ逆浸透膜は、それぞれ食
塩除去率が１０〜６０％のものであることを特徴とする
膜分離装置。(3) The apparatus according to claim 1 or 2, wherein each of the first and second loose reverse osmosis membranes has a salt removal rate of 10 to 60%. Membrane separation equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60040945A JPS61200813A (en) | 1985-03-01 | 1985-03-01 | Membrane separation apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60040945A JPS61200813A (en) | 1985-03-01 | 1985-03-01 | Membrane separation apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS61200813A true JPS61200813A (en) | 1986-09-05 |
Family
ID=12594645
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60040945A Pending JPS61200813A (en) | 1985-03-01 | 1985-03-01 | Membrane separation apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS61200813A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63205105A (en) * | 1987-02-20 | 1988-08-24 | Nitto Electric Ind Co Ltd | Concentration of aqueous solution of low molecular weight organic compound by means of membrane |
| JPH01171688A (en) * | 1987-12-25 | 1989-07-06 | Showa Eng Kk | Treatment of organic waste liquid |
| WO2003092870A1 (en) | 2002-05-02 | 2003-11-13 | City Of Long Beach | Two stage nanofiltration seawater desalination system |
| CN105621770A (en) * | 2014-11-04 | 2016-06-01 | 中国石油化工股份有限公司 | High salinity wastewater zero-emission method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5328082A (en) * | 1976-08-18 | 1978-03-15 | Ebara Infilco Co Ltd | Membrane separating method |
| JPS54124875A (en) * | 1978-03-23 | 1979-09-28 | Mitsui Toatsu Chem Inc | Concentrating solution |
| JPS5867303A (en) * | 1981-07-10 | 1983-04-21 | ネ−デルランズ・セントラル・オルガニザテイ・ボ−ル・トゲパ−スト・ナチユ−ルベツトンシヤベリツク・オンデルゾ−ク | Method and apparatus for concentrating solution by reverse osmosis |
-
1985
- 1985-03-01 JP JP60040945A patent/JPS61200813A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5328082A (en) * | 1976-08-18 | 1978-03-15 | Ebara Infilco Co Ltd | Membrane separating method |
| JPS54124875A (en) * | 1978-03-23 | 1979-09-28 | Mitsui Toatsu Chem Inc | Concentrating solution |
| JPS5867303A (en) * | 1981-07-10 | 1983-04-21 | ネ−デルランズ・セントラル・オルガニザテイ・ボ−ル・トゲパ−スト・ナチユ−ルベツトンシヤベリツク・オンデルゾ−ク | Method and apparatus for concentrating solution by reverse osmosis |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63205105A (en) * | 1987-02-20 | 1988-08-24 | Nitto Electric Ind Co Ltd | Concentration of aqueous solution of low molecular weight organic compound by means of membrane |
| JPH01171688A (en) * | 1987-12-25 | 1989-07-06 | Showa Eng Kk | Treatment of organic waste liquid |
| WO2003092870A1 (en) | 2002-05-02 | 2003-11-13 | City Of Long Beach | Two stage nanofiltration seawater desalination system |
| EP1499424A1 (en) * | 2002-05-02 | 2005-01-26 | City of Long Beach | Two stage nanofiltration seawater desalination system |
| EP1499424A4 (en) * | 2002-05-02 | 2005-12-21 | City Of Long Beach | Two stage nanofiltration seawater desalination system |
| CN105621770A (en) * | 2014-11-04 | 2016-06-01 | 中国石油化工股份有限公司 | High salinity wastewater zero-emission method |
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