JPS644802B2 - - Google Patents
Info
- Publication number
- JPS644802B2 JPS644802B2 JP55013918A JP1391880A JPS644802B2 JP S644802 B2 JPS644802 B2 JP S644802B2 JP 55013918 A JP55013918 A JP 55013918A JP 1391880 A JP1391880 A JP 1391880A JP S644802 B2 JPS644802 B2 JP S644802B2
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- pressure
- membrane
- backwashing
- back pressure
- 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
Links
- 239000007788 liquid Substances 0.000 claims description 71
- 239000012528 membrane Substances 0.000 claims description 55
- 238000000034 method Methods 0.000 claims description 31
- 238000011001 backwashing Methods 0.000 claims description 26
- 238000001914 filtration Methods 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 12
- 239000000126 substance Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 10
- 230000000694 effects Effects 0.000 claims description 6
- 238000004140 cleaning Methods 0.000 claims description 4
- 239000003814 drug Substances 0.000 claims description 2
- 229940079593 drug Drugs 0.000 claims description 2
- 239000013043 chemical agent Substances 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 21
- 238000011282 treatment Methods 0.000 description 17
- 239000012530 fluid Substances 0.000 description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 8
- 239000004576 sand Substances 0.000 description 5
- 239000012466 permeate Substances 0.000 description 4
- 238000002203 pretreatment Methods 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 3
- 230000003204 osmotic effect Effects 0.000 description 3
- 238000001223 reverse osmosis Methods 0.000 description 3
- 239000013535 sea water Substances 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 239000003599 detergent Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 238000009287 sand filtration Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 239000005909 Kieselgur Substances 0.000 description 1
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000002788 crimping Methods 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000012982 microporous membrane Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 230000010287 polarization Effects 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000004094 surface-active agent Substances 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
- B01D61/04—Feed pretreatment
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
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)
- Filtration Of Liquid (AREA)
Description
【発明の詳細な説明】
本発明は、過工程を前処理工程とし脱塩など
の処理に圧力を使用する透過膜処理工程におい
て、透過膜処理工程から排出される流体の圧力を
利用して、該透過膜処理に付される被処理液中の
懸濁浮遊物質などを除去する過装置における
材を洗浄再生する方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention utilizes the pressure of the fluid discharged from the permeable membrane treatment process in a permeable membrane treatment process in which the overstep is a pretreatment process and pressure is used for treatments such as desalination. The present invention relates to a method for cleaning and regenerating materials in a filtration device that removes suspended substances in a liquid to be treated that is subjected to the permeable membrane treatment.
最近、透過膜処理として逆浸透圧法、ウルトラ
フイルトレーシヨン法等が脱塩、脱有機物などに
効果的に利用されているが、これらの処理におい
ては数Kgｆ／cm2乃至数10Kgｆ／cm2の圧力を必要と
している。例えば逆浸透圧法においては、その被
処理液における浸透圧の数倍の圧力を運転圧とし
てその被処理液を加圧することによつて、半透膜
を経て透過水を得るわけであるが、この際濃縮液
は高圧であつて最終的には減圧弁によつて常圧に
減圧される。しかしながら、従来この濃縮液の有
する高圧の利用法としては、特公昭48−988号公
報にみられるごとき、タービンを利用し圧力を速
度エネルギに変換して高圧エネルギを回収し、こ
のエネルギをもつてポンプを駆動させる方法があ
る。この回収動力の利用に際しては、メインを流
れる液の送水とか、あるいは特開昭54−10284号
公報にみられるようにメインを流れる液の循環に
利用されている。このような利用法は、タービン
を利用して高圧エネルギを回収するものである
が、本発明は、高圧流体の高圧を直接利用しよう
とするものである。利用される流体の圧力は、そ
のままあるいは減圧して適度の圧力にしてから利
用することができる。 Recently, permeable membrane treatments such as reverse osmosis and ultrafiltration methods have been effectively used for desalination and removal of organic matter, but in these treatments, the Needs pressure. For example, in the reverse osmosis method, permeate water is obtained through a semi-permeable membrane by pressurizing the liquid to be treated at an operating pressure several times the osmotic pressure of the liquid to be treated. The concentrated liquid is under high pressure and is finally reduced to normal pressure by a pressure reducing valve. However, the conventional method of utilizing the high pressure of this concentrated liquid is as shown in Japanese Patent Publication No. 1988-988, in which the high pressure energy is recovered by converting the pressure into velocity energy using a turbine, and this energy is then used. There is a way to drive the pump. When this recovered power is utilized, it is used to transport the liquid flowing through the main, or to circulate the liquid flowing through the main as seen in Japanese Patent Laid-Open No. 54-10284. Although such usage uses a turbine to recover high-pressure energy, the present invention attempts to directly utilize the high pressure of high-pressure fluid. The pressure of the fluid used can be used as is or after being reduced to an appropriate pressure.
透過膜処理においては、液中に存する懸濁性物
質、コロイド性物質などの存在が大きな問題とな
り、これらの膜面への付着は、その透過水量の低
下へと大きく影響するとともに、濃度分極の原因
ともなつて、有効圧力差の低下、及び膜の破損を
招くから、できる限り十分な前処理によつて被処
理液中の懸濁浮遊物質などの除去が望まれるとと
もに、膜透過水もできる限り多く回収することが
望まれる。 In permeable membrane treatment, the presence of suspended substances and colloidal substances in the liquid poses a major problem, and their adhesion to the membrane surface has a significant effect on reducing the amount of permeated water and also causes concentration polarization. This may also lead to a decrease in the effective pressure difference and damage to the membrane, so it is desirable to remove suspended solids from the liquid to be treated by as sufficient a pretreatment as possible, and at the same time, water permeates through the membrane. It is desirable to collect as much as possible.
本発明は、透過膜処理において系外へ排出され
る高圧系の液体の圧力を有効に利用して、透過膜
工程によつて処理されるべき被処理液の過工程
における材の逆洗洗浄を遂行して材に付着す
る汚染物を除去するもので、かくて被処理液の前
処理を効果的に行い、膜への影響を極小にし、透
過膜プロセスの効率を向上させる有効な背圧利用
方法を提供することを目的とするものである。 The present invention effectively utilizes the pressure of the high-pressure liquid discharged outside the system in the permeable membrane process to backwash the material during the passing process of the liquid to be treated in the permeable membrane process. This method effectively pre-treats the liquid to be treated, minimizes the effect on the membrane, and improves the efficiency of the permeable membrane process. The purpose is to provide a method.
本発明は、圧力を使用する透過膜処理におい
て、該透過膜処理工程における高圧系液体の全部
又は一部を使用し、その液体が持つている比較的
高圧のエネルギをそのまま、前処理において使用
した過装置の材の逆洗に利用することによつ
て、常時被処理液の前処理を円滑に行ない透過膜
処理工程の処理効果を高度に維持しようとするも
のである。 In permeation membrane treatment using pressure, the present invention uses all or part of the high-pressure liquid in the permeation membrane treatment step, and uses the relatively high-pressure energy of the liquid as it is in pretreatment. By using it for backwashing the material of the permeation device, the pretreatment of the liquid to be treated can be carried out smoothly at all times and the treatment effect of the permeation membrane treatment process can be maintained at a high level.
透過膜処理工程から排出される液体の圧力は数
Kgｆ／cm2乃至数10Kgｆ／cm2の圧力であつて、例え
ば逆浸透圧法においては、その被処理液の浸透圧
の数倍の圧力を運転圧としてその被処理液を加圧
することによつて、半透膜を経て透過水を得るわ
けであるが、この際濃縮液は少なくとも15Kgｆ／
cm2の高圧である。海水に至つては浸透圧が約25Kg
ｆ／cm2であるから被処理海水の加圧は自と、50〜
70Kgｆ／cm2となり、系外へ排出される濃縮液の圧
力は少なくとも45Kgｆ／cm2で相当の高圧と言え
る。 The pressure of the liquid discharged from the permeable membrane treatment process is
Kgf/cm 2 to several tens of Kgf/cm 2 , for example, in reverse osmosis, the operating pressure is several times the osmotic pressure of the liquid to be treated, and the liquid to be treated is pressurized. , the permeated water is obtained through a semi-permeable membrane, but at this time the concentrated liquid is at least 15Kgf/
It has a high pressure of cm2 . The osmotic pressure of seawater is approximately 25Kg.
f/ cm2 , so the pressure of the seawater to be treated is 50~
The pressure of the concentrated liquid discharged to the outside of the system is at least 45 Kgf/cm 2 , which can be said to be a considerably high pressure.
また、ウルトラフイルトレーシヨン法あるいは
マイクロポーラス膜を利用した膜過法において
は膜が一種の篩として利用される透過膜法であ
り、加える圧力は２〜７Kgｆ／cm2の低圧でよく、
その系外排出濃縮液の圧力は通常１〜５Kgｆ／cm2
程度である。この圧力の利用は低圧であるが故に
また考えられていない。特にウルトラフイルトレ
ーシヨン法の場合には、有機質含有液の処理に利
用される可能性が大きく、高分子物質である蛋白
質の濃縮、油水の分離、パルプ廃水中の高分子リ
グニンの分別濃縮、廃水中のコロイド性高分子機
物の分離濃縮などにも利用することができるが、
この工程において使用した圧力も全く回収利用さ
れずに廃棄されているのが現状である。 In addition, in the ultrafiltration method or the membrane filtration method using a microporous membrane, the membrane is used as a kind of sieve, and the pressure applied may be as low as 2 to 7 Kgf/ cm2 .
The pressure of the concentrated liquid discharged outside the system is usually 1 to 5 kgf/cm 2
That's about it. The use of this pressure is also not considered because of the low pressure. In particular, the ultrafiltration method has great potential to be used in the treatment of organic-containing liquids, such as the concentration of high-molecular proteins, separation of oil and water, fractional concentration of high-molecular lignin in pulp wastewater, and wastewater. It can also be used for separating and concentrating colloidal polymer substances inside.
At present, the pressure used in this process is not recovered or used at all and is discarded.
また、これら透過膜処理工程から排出される高
圧濃縮液（膜側残留液と同じ）の量は加圧水量の
１／２乃至1/5程度であることが多いが、海水を逆浸
透圧法によつて処理する場合には、加圧水量の2/
３程度であり場合によつては9/10程度に及ぶこと
もある。このような高圧の膜側残留液は、精密
過処理などの前処理からの処理水が濃縮されたも
のであるから、懸濁浮遊物はほとんど存在せず濃
縮された流体とは言え、極めて清澄なものであ
る。とくに濃縮度が余り進んでいない前記のよう
な加圧水量の2/3とか9/10が膜側残留液として排
出される場合にはほとんど過処理された液体と
変わらない。このような清澄かつ圧力を保有する
流体をそのまま廃棄することは極めて大きな損失
である。透過膜分離プロセスを利用するに当つて
は、多くの場合、被処理液の前処理を行なつてか
ら透過膜分離プロセスへ供給するが、この前処理
としての過工程においては定期的に材を清澄
な過水を加圧して逆洗し、材層の表面あるい
は材の細孔内、材間に付着した汚染物を除去
て再生を行なつているのが実状である。 In addition, the amount of high-pressure concentrated liquid (same as the residual liquid on the membrane side) discharged from these permeable membrane treatment processes is often about 1/2 to 1/5 of the amount of pressurized water, but seawater is When processing with water, 2/2 of the amount of pressurized water
It is about 3, and in some cases it can reach about 9/10. This kind of high-pressure residual liquid on the membrane side is concentrated treated water from pre-treatments such as precision overtreatment, so there are almost no suspended solids, and although it is a concentrated fluid, it is extremely clear. It is something. In particular, when 2/3 or 9/10 of the amount of pressurized water is discharged as membrane-side residual liquid, as mentioned above, where the degree of concentration has not progressed very much, it is almost the same as over-treated liquid. It would be a huge loss to dispose of such a clear and pressurized fluid as it is. When using a permeable membrane separation process, in most cases, the liquid to be treated is pretreated before being supplied to the permeable membrane separation process, but during this pretreatment process, the material is periodically removed. In reality, regeneration is carried out by backwashing with pressurized clear water to remove contaminants that have adhered to the surface of the material layer, within the pores of the material, or between the materials.
この材の逆洗に、前記するごとき清澄の高圧
膜側残留液を利用することは極めて合理的であ
る。前処理工程にて採用される過装置の一般的
なものは、砂、活性炭を材とする加圧式あるい
は重力式砂過機、珪藻土を利用したプレコート
過機、細孔の樹脂あるいはステンレス製のカー
トリツジフイルターなどである。従来法によるこ
れらの逆洗工程は、通常は清澄な過水を別途に
設けるポンプによつて加圧して行なわれるが、本
発明は清澄な過水の代りに、すでに前処理によ
つて過され清澄化した膜分離プロセスの膜側残
留液を利用するものであり、ポンプを利用せず、
その自らの有する圧力を利用するものであるか
ら、従来のごとく洗浄のための逆洗ポンプを設備
し、過したい過処理水を徒に使用する必要は
全くないのである。 It is extremely rational to use the clear residual liquid on the high-pressure membrane side as described above for backwashing this material. Common filtration equipment used in the pre-treatment process is a pressurized or gravity-type sand filtration machine made of sand or activated carbon, a pre-coat filtration machine made of diatomaceous earth, a pore resin or stainless steel carton. Such as Toritsuji Filter. These backwashing steps according to conventional methods are usually carried out by pressurizing clear filtered water with a separately provided pump, but the present invention uses water that has already been filtered through pre-treatment instead of clear filtered water. This method uses the clarified residual liquid on the membrane side of the membrane separation process, and does not use a pump.
Since it utilizes its own pressure, there is no need to install a backwash pump for cleaning as in the past and use overtreated water unnecessarily.
膜分離プロセスにおける膜側残留液量のみによ
つては過機の逆洗を完遂できない場合もあるの
で適当な清澄水の補給が必要なときもある。ま
た、高圧の膜側残留液による逆洗に当つては気体
の導入も可能で、ガス−液混合流体によつて逆洗
効果を助長することもできる。 Depending on the amount of liquid remaining on the membrane side in the membrane separation process, it may not be possible to complete the backwashing of the filter, so it may be necessary to replenish an appropriate amount of clear water. Further, when backwashing is performed using the high-pressure residual liquid on the membrane side, it is also possible to introduce gas, and the backwashing effect can also be promoted by using a gas-liquid mixed fluid.
次に本発明の実施例を第１図を参照しつつ説明
すると、被処理水は管路１を経て砂過装置Ａに
供給され過される。この場合、通常材として
は平均粒径0.4〜0.6mmの珪砂を使用する。過速
度はLVとして５〜15ｍ／ｈであるが、通常は約
６〜７ｍ／ｈである。液は管路２を経て砂過
処理水槽Ｂに貯留された後、管路３を経て送液ポ
ンプＰ−１によつて加圧され、管路４，５を経て
精密過装置Ｃ−１に至りここで過される。精
密過装置Ｃ−１のメデア（材）は逆洗によつ
て再生し得るもの、すなわち材質としては多数の
樹脂を固結させたもの、あるいは焼結金属、網状
体、多数の網状体を圧着せしめたものなど逆洗可
能なメデアを利用する。 Next, an embodiment of the present invention will be described with reference to FIG. 1. Water to be treated is supplied to a sand filter device A through a pipe 1 and filtered. In this case, silica sand with an average particle size of 0.4 to 0.6 mm is usually used as the material. The overspeed is 5 to 15 m/h as LV, but usually about 6 to 7 m/h. After the liquid passes through pipe 2 and is stored in sand filter treatment tank B, it passes through pipe 3 and is pressurized by liquid sending pump P-1, and then passes through pipes 4 and 5 to precision filtration equipment C-1. This is where I end up. The media (material) of the precision filtering device C-1 can be recycled by backwashing, i.e., it can be made by solidifying many resins, sintered metal, mesh, or crimping many meshes. Use media that can be backwashed, such as those that have been washed.
次いで液は、管路６，７を経て昇圧ポンプＰ
−２によつて更に昇圧されて、管路８を経て透過
膜装置Ｄへ圧送される。透過膜装置Ｄにおいて
は、膜透過液と膜側残留液（濃縮液とも云
う）に分離される。膜側残留液は本発明におい
て利用する高圧の清澄な液体で、系内圧力調整弁
ｊによつて減圧され、管路１１を経て系外へ排出
される。以上の間、各経路上の弁ａ，ｂおよびｅ
は全開であり、その他の弁は全閉となつている。
以上が透過膜システムの正常時の運転状況であ
る。 The liquid then passes through pipes 6 and 7 to the boost pump P.
-2, the pressure is further increased, and the pressure is sent to the permeable membrane device D via the pipe line 8. In the permeable membrane device D, the permeated liquid is separated into a membrane-side residual liquid (also referred to as a concentrated liquid). The residual liquid on the membrane side is a high-pressure clear liquid used in the present invention, and its pressure is reduced by the system pressure regulating valve j, and it is discharged to the outside of the system through the pipe line 11. During the above, valves a, b and e on each path
is fully open, and the other valves are fully closed.
The above is the normal operating status of the permeable membrane system.
さて、長期に運転が継続されるにつれて精密
過装置Ｃ−１におけるメデアは目詰まりして過
の圧力損失が増大する。そこで、所定の圧力損失
に至れば自動あるいは手動によつて弁の開閉の切
替えを行なう。即ち、送液ポンプＰ−１からの加
圧流体を管路４，１７および１３を経て並列配備
された予備の精密過装置Ｃ−２へ流入せしめ、
その液を管路１２，１６および７を経て昇圧ポ
ンプＰ−２へ送り昇圧せしめて管路８を経て透過
膜装置Ｄへ加圧下に送液する。透過膜装置Ｄ内の
圧力は系内圧力調整弁ｊの調整によつて所定圧に
維持される。管路１０を経る高圧の膜側残留液
は系内圧力調整弁ｊによつて減圧され、管路１
５，６を経て精密過装置Ｃ−１のメデアを逆洗
し、管路１８を経て系外へ排出される。以上の間
弁ｃ，ｄ，ｈおよびｉは全開であり、他は全閉と
なつている。 Now, as the operation continues for a long period of time, the media in the precision filtration device C-1 becomes clogged and excessive pressure loss increases. Therefore, when a predetermined pressure loss is reached, the valve is automatically or manually switched to open and close. That is, the pressurized fluid from the liquid pump P-1 is made to flow through the pipes 4, 17 and 13 into the spare precision filter device C-2 arranged in parallel,
The liquid is sent to the booster pump P-2 via pipes 12, 16 and 7 to increase the pressure, and then sent to the permeable membrane device D via the pipe 8 under pressure. The pressure inside the permeable membrane device D is maintained at a predetermined pressure by adjusting the system pressure regulating valve j. The high pressure residual liquid on the membrane side passing through the pipe line 10 is reduced in pressure by the system pressure regulating valve j, and
5 and 6, the media of the precision filtration device C-1 is backwashed, and is discharged to the outside of the system through a pipe 18. During the above period, valves c, d, h, and i are fully open, and the others are fully closed.
次に精密過装置Ｃ−２のメデアが目詰まりす
ると、その圧力を自動あるいは人為的に検出し
て、自動あるいは手動によつて精密過装置Ｃ−
２の逆洗工程に、そして逆洗を終了した精密過
装置Ｃ−１は通常の過工程に移る。 Next, when the media of the precision filter C-2 becomes clogged, the pressure is automatically or manually detected and the precision filter C-2 is automatically or manually detected.
After completing the backwashing process, the precision filtration apparatus C-1 moves to the normal filtration process.
まず送液ポンプＰ−１から移送される被処理液
は、管路４，５を経て精密過装置Ｃ−１に至
り、その液は管路６，７を経て昇圧ポンプＰ−
２により更に昇圧されて管路８を経て透過膜装置
Ｄに加圧下に送液される。透過膜装置Ｄからの膜
透過液は管路９を経て系外へ排出され、膜側残
留液は管路１０を経て系内圧力調整弁ｊにより
減圧された後、管路１２を経て精密過装置Ｃ−
２に送られ、これを逆洗して管路１３，１４を経
て系外へ排出される。以上の間弁ａ，ｂ，ｆ，ｇ
は全開で、他は全閉である。なお、管路１１およ
び弁ｅは特に精密過装置Ｃ−１またはＣ−２の
逆洗を要しないときの膜側残留液の排出経路で
あり、また自動、手動による弁切替え時のそれぞ
れ経路およびリリーフ弁として作用するものであ
つて必須のものではない。 First, the liquid to be treated transferred from the liquid transfer pump P-1 passes through pipes 4 and 5 to reach the precision filter C-1, and the liquid passes through pipes 6 and 7 to the booster pump P-1.
2, the liquid is further pressurized and sent to the permeable membrane device D through the pipe line 8 under pressure. The membrane permeate liquid from the permeable membrane device D is discharged to the outside of the system via pipe 9, and the residual liquid on the membrane side passes through pipe 10 and is depressurized by the system pressure regulating valve j, and then passes through pipe 12 to the precision membrane. Device C-
2, it is backwashed and discharged to the outside of the system via pipes 13 and 14. Between the above valves a, b, f, g
are fully open and the others are fully closed. The pipe line 11 and the valve e are the discharge route for the residual liquid on the membrane side especially when backwashing of the precision filtration device C-1 or C-2 is not required, and the route and the valve e are respectively used when the valve is switched automatically or manually. It acts as a relief valve and is not essential.
以上においては、メデアを取り出すことなく逆
洗を行なう方法を説明したが、別にバツチ式の洗
浄設備を設けメデアを取り出してはその洗浄設備
に取り付け、（その間洗浄ずみのメデアを過設
備に収納して定常運転に入り、）高圧膜側残留液
で逆洗してもよい。 The above explained the method of backwashing without taking out the media, but it is also possible to install separate batch-type washing equipment, take out the media, attach it to the washing equipment, and store the washed media in the backwashing equipment. () to start steady operation, and backwash with the residual liquid on the high-pressure membrane side.
一方、高圧の膜側残留液によつて精密過装
置Ｃ−１又はＣ−２のメデアを逆洗する際、メデ
アの汚染原因物質あるいは目詰まり原因物質に対
して化学的に不活性なガス体又はこれらの原因物
質に対し酸化力を有するガス体、例えばN2、
Cl2、O3、O2などを利用し、第２図に示す如くこ
れを管路１９を経て気−液エゼクタＥを介して流
入せしめ、メデアをガス−液混合流体で洗浄する
ことができる。 On the other hand, when backwashing the media of precision filtration equipment C-1 or C-2 with high-pressure membrane-side residual liquid, a gaseous substance that is chemically inert against substances that cause contamination or clogging of the media is used. Or a gaseous body that has oxidizing power against these causative substances, such as N 2 ,
Using Cl 2 , O 3 , O 2 , etc., the medium can be washed with the gas-liquid mixed fluid by flowing it through the pipe 19 and through the gas-liquid ejector E as shown in FIG. .
なお、ガス体の代りに管路１９から逆洗に不足
分の液体を供給することもでき、そのときにはＥ
として液−液エゼクタを利用することができる。 In addition, it is also possible to supply the insufficient amount of liquid for backwashing from the pipe line 19 instead of the gas, and in that case, the E
A liquid-liquid ejector can be used as a liquid-liquid ejector.
また上記メデア洗浄の際に薬剤処理を必要とす
るときには、やはり管路１９より適当な薬品を供
給しメデアの逆洗を円滑に行なうことができる。
例えば次亜塩素酸ソーダ液、ホルマリン液、過酸
化物などの溶液あるいは界面活性剤を含む洗剤、
酵素洗剤、酸、アルカリ剤などを利用することも
できる。あるいは、上記ガス体と薬剤溶液等の液
体の両方を同時に使用してもよい。 Further, when chemical treatment is required during the media cleaning, an appropriate chemical can be supplied from the conduit 19 to smoothly backwash the media.
For example, detergents containing solutions such as sodium hypochlorite solution, formalin solution, peroxide, or surfactants,
Enzyme detergents, acids, alkaline agents, etc. can also be used. Alternatively, both the gas and a liquid such as a drug solution may be used simultaneously.
また、上記メデアの逆洗に際して加温が効果的
である場合には、透過膜装置Ｄの膜側残留液の
流出口と精密過装置Ｃ−１又はＣ−２の逆洗流
体入口の間の経路に加熱圏を設けるか、精密過
装置Ｃ−１又はＣ−２自体を加熱し得る機構を設
けてもよい。 In addition, if heating is effective when backwashing the media, the temperature between the membrane-side residual liquid outlet of permeation membrane device D and the backwash fluid inlet of precision filtration device C-1 or C-2 may be increased. A heating zone may be provided in the path, or a mechanism may be provided that can heat the precision heating device C-1 or C-2 itself.
以上の説明においては精密過装置Ｃ−１又は
Ｃ−２の逆洗について示したが、同様の方法によ
り砂過装置Ａのメデアの逆洗に利用することも
できる。その際には通常逆洗水量が不足するので
別途逆洗用水を補給する必要がある。この場合に
も第２図について示したように管路１９からたと
えばガス体を導入して逆洗効果を高めることがで
きる。また精密過装置は、３台以上並列に配備
し、過工程と逆洗工程を順番に切替えて使用し
てもよい。 In the above explanation, the backwashing of the precision filtration device C-1 or C-2 has been described, but the same method can also be used for backwashing the media of the sand filtration device A. In this case, the amount of backwash water is usually insufficient, so it is necessary to separately supply backwash water. In this case as well, the backwashing effect can be enhanced by introducing, for example, a gaseous body through the conduit 19, as shown in FIG. Further, three or more precision washing devices may be arranged in parallel and used by switching over processing and backwashing steps in order.
このように本発明によるときには、膜分離プロ
セスから排出される清澄な加圧液を、過工程に
おけるメデアの逆洗に際し、直接的にその加圧液
の保有するエネルギを極めて効率良く且つ容易に
利用できるので、前処理としての過工程を効果
的に従つて膜分離プロセスを高い効率で実施で
き、また逆洗専用ポンプ等の設備が省略できるば
かりでなく、逆洗用の清澄水も不要となり、そ
の操作も簡便であり、設備費、運転経費ともに著
しく節減できるなどの利点を有するものである。 As described above, according to the present invention, the clear pressurized liquid discharged from the membrane separation process can be used to directly utilize the energy possessed by the pressurized liquid extremely efficiently and easily when backwashing the media in the previous step. As a result, the membrane separation process can be carried out with high efficiency by effectively following the filtration process as pre-treatment, and not only can equipment such as pumps exclusively for backwashing be omitted, but also clear water for backwashing is no longer necessary. Its operation is simple, and it has the advantage of significantly reducing both equipment costs and operating costs.
図面は本発明の実施例を示し、第１図は全体系
統説明図、第２図はエゼクタを利用する場合の部
分系統説明図である。
Ａ……砂過装置、Ｂ……処理水槽、Ｃ−１，
Ｃ−２……精密過装置、Ｄ……透過膜装置、Ｅ
……エゼクタ、Ｐ−１……送液ポンプ、Ｐ−２…
…昇圧ポンプ、ａ乃至ｊ……弁、１乃至１９……
管路、……膜透過液、……膜側残留液。
The drawings show an embodiment of the present invention, with FIG. 1 being an explanatory diagram of the entire system, and FIG. 2 being an explanatory diagram of a partial system when an ejector is used. A... Sand filter device, B... Treatment water tank, C-1,
C-2... Precision filter device, D... Permeable membrane device, E
...Ejector, P-1...Liquid pump, P-2...
...boosting pumps, a to j... valves, 1 to 19...
Pipe line, ...membrane permeate liquid, ...membrane side residual liquid.
Claims (1)
ロセスにおいて、前記膜分離プロセスから排出さ
れる膜側残留液の圧力を前記過工程における
材の逆洗洗浄に利用することを特徴とする膜分離
プロセスにおける背圧利用法。 ２ 前記逆洗洗浄工程が、前記膜側残留液を管路
により精密過装置へ供給、通液して処理される
ものである特許請求の範囲第１項記載の背圧利用
法。 ３ 前記過工程が、２台又は３台以上の前記精
密過装置を並列的に使用して行なわれるもので
あつて、前記過工程と前記逆洗洗浄工程がそれ
ぞれ交互又は順番に切替えて処理されるものであ
る特許請求の範囲第２項記載の背圧利用法。 ４ 前記逆洗洗浄工程が、前記膜側残留液に対し
前記精密過装置の材の汚染原因物質又は閉塞
原因物質に対し化学的又は物理的洗浄作用を有す
るガス体及び／又は薬剤を混合して処理されるも
のである特許請求の範囲第２項又は第３項記載の
背圧利用法。 ５ 前記ガス体又は薬剤の混合工程が、気−液エ
ゼクタ及び／又は液−液エゼクタを使用して処理
されるものである特許請求の範囲第４項記載の背
圧利用法。[Scope of Claims] 1. In a membrane separation process having a pass step as a pretreatment step, the pressure of the residual liquid on the membrane side discharged from the membrane separation process is used for backwashing of the material in the pass step. A method of utilizing back pressure in membrane separation processes. 2. The back pressure utilization method according to claim 1, wherein the backwashing step is performed by supplying the residual liquid on the membrane side to a precision filtration device through a pipe and passing the liquid therethrough. 3. The above-mentioned passing process is carried out using two or more of the above-mentioned precision passing equipment in parallel, and the above-mentioned passing process and the backwashing process are respectively switched alternately or sequentially. 2. A method of utilizing back pressure according to claim 2. 4. The backwashing step includes mixing a gaseous body and/or a chemical agent having a chemical or physical cleaning effect on the contamination-causing substances or blockage-causing substances of the material of the precision filtration device into the membrane-side residual liquid. 3. The method of utilizing back pressure according to claim 2 or 3, wherein the method is processed. 5. The back pressure utilization method according to claim 4, wherein the step of mixing the gas or the drug is performed using a gas-liquid ejector and/or a liquid-liquid ejector.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1391880A JPS56111006A (en) | 1980-02-07 | 1980-02-07 | Method for utilization of back pressure in membrane separating process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1391880A JPS56111006A (en) | 1980-02-07 | 1980-02-07 | Method for utilization of back pressure in membrane separating process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS56111006A JPS56111006A (en) | 1981-09-02 |
| JPS644802B2 true JPS644802B2 (en) | 1989-01-26 |
Family
ID=11846544
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1391880A Granted JPS56111006A (en) | 1980-02-07 | 1980-02-07 | Method for utilization of back pressure in membrane separating process |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS56111006A (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5942011A (en) * | 1982-09-02 | 1984-03-08 | Mitsui Eng & Shipbuild Co Ltd | Washing method of pretreatment filter in water making device with reverse osmotic membrane |
| JPS61139702U (en) * | 1985-02-19 | 1986-08-29 | ||
| JPS6295702U (en) * | 1985-12-02 | 1987-06-18 | ||
| JPS6443398A (en) * | 1987-08-11 | 1989-02-15 | S I Ii Kk | Waste water regenerating apparatus |
| DE19520913A1 (en) * | 1995-06-08 | 1996-12-12 | Schael Wilfried | Method and device for water treatment according to the principle of reverse osmosis |
| US6120688A (en) * | 1997-02-25 | 2000-09-19 | Zenon Environmental, Inc. | Portable reverse osmosis unit for producing drinking water |
| FR2781168B1 (en) | 1998-07-17 | 2000-09-15 | Polymem | WATER TREATMENT PROCESS AND INSTALLATION |
| JP2013163141A (en) * | 2012-02-09 | 2013-08-22 | Toshiba Corp | Membrane filtration system |
| WO2014007262A1 (en) * | 2012-07-02 | 2014-01-09 | 東レ株式会社 | Fresh-water manufacturing device and fresh-water manufacturing method |
-
1980
- 1980-02-07 JP JP1391880A patent/JPS56111006A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS56111006A (en) | 1981-09-02 |
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