JPS62204812A - Separation and concentration device for activated sludge - Google Patents
Separation and concentration device for activated sludgeInfo
- Publication number
- JPS62204812A JPS62204812A JP61047923A JP4792386A JPS62204812A JP S62204812 A JPS62204812 A JP S62204812A JP 61047923 A JP61047923 A JP 61047923A JP 4792386 A JP4792386 A JP 4792386A JP S62204812 A JPS62204812 A JP S62204812A
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- raw water
- concentration
- separation
- pressure vessel
- 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
- 238000000926 separation method Methods 0.000 title claims abstract description 24
- 239000010802 sludge Substances 0.000 title claims abstract description 18
- 239000012528 membrane Substances 0.000 claims abstract description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000000919 ceramic Substances 0.000 claims abstract description 7
- 238000005273 aeration Methods 0.000 abstract description 7
- 239000007788 liquid Substances 0.000 abstract description 5
- 239000011148 porous material Substances 0.000 abstract description 4
- 239000012466 permeate Substances 0.000 description 6
- 230000004907 flux Effects 0.000 description 5
- 239000012141 concentrate Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 229910010293 ceramic material Inorganic materials 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 241000588724 Escherichia coli Species 0.000 description 1
- 239000011247 coating layer Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 239000010800 human waste Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000010410 layer Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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
- Activated Sludge Processes (AREA)
- Treatment Of Sludge (AREA)
- Filtration Of Liquid (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
（１）産業上の利用分野
本発明は下水、し尿、産業廃水等の原水の活性汚泥の分
ｇＩＩ濃ｗＪ装置に関する。DETAILED DESCRIPTION OF THE INVENTION (1) Industrial Application Field The present invention relates to an apparatus for separating activated sludge from raw water such as sewage, human waste, and industrial wastewater.
（２）従来の技術
出願人は先にこの種装置に関して、第６図示のｍｌｌメ
ツ ｎ −＝ニアｓ＋ ＋百、に舊Ｊギー信積／ａ）し
分離濃縮装置（ｂ）とこれらを接続し途中にポンプ（Ｃ
）を介在した管路（ｃｉ）とからなり、該分１１１ｔｉ
ＫｄＨｉｉ！（ｂ） ｌ＊ｆ５７図ＥｔＡｊｔｊｓ８ｕ
示ノ如＜ 略丁字形のパイプ体（ｅ）と該パイプ体Ｃｅ
’）内に根部においてシールド固定した分離濃縮膜体（
ｆ）とからなり、該分離濃縮膜体（ｆ）は先端が閉塞し
た管状体で、その周壁をセラミック多孔体により形成し
、ばっ気槽（ａ）から原水をポンプ（Ｃ）により管路（
ｄ）を経て分離濃縮装置（ｂ）のパイプ体（ｅ）内に流
すと、該原水が管状の分離濃縮膜体（ｆ）の外側表面上
を流れて該膜体（ｆ）により活性汚泥が分離され、該膜
体（ｆ）を透過したを透過液は該膜体（ｆ）内を流れて
管路（ｇ）内に至り、又活性汚泥の濃縮液は管路（ｈ）
内に至・るようにしたものを提案した（特開昭６０−２
１２３００号公報）。(2) Conventional technology Applicant previously related to this type of device as shown in Fig. 6, which is connected to the separation/concentration device (b). The pump (C)
), with a corresponding 111ti
KdHii! (b) l*f57 diagram EtAjtjs8u
As shown < Approximately T-shaped pipe body (e) and the pipe body Ce
Separation and concentration membrane body (
f), the separation/concentration membrane body (f) is a tubular body with a closed end, the peripheral wall of which is formed of a porous ceramic material, and the raw water is passed from the aeration tank (a) to the pipe (C) by means of a pump (C).
d) and into the pipe body (e) of the separation/concentration device (b), the raw water flows over the outer surface of the tubular separation/concentration membrane body (f), and activated sludge is converted into activated sludge by the membrane body (f). The permeated liquid that has been separated and permeated through the membrane body (f) flows through the membrane body (f) and reaches the pipe (g), and the concentrated activated sludge liquid flows through the pipe (h).
proposed a method that would reach the innermost part of the
12300).
尚、第６図において（ｇ）は透過液の管路、（ｈ）は活
性汚泥の濃縮液の管路、（ｉ）はその環流管路、（ｊ）
は逆止弁を示す。In Fig. 6, (g) is the permeate pipe, (h) is the activated sludge concentrate pipe, (i) is the reflux pipe, and (j) is the pipe for the activated sludge concentrate.
indicates a check valve.
（３）発明がＭりＩＬ Ｌ、 Ｊ−うとするｒ！’Ａ頴
へ発明者はその後この従来装置について実験をした結果
、前記膜体（ｆ）の外側表面の原水の線速度が所定の値
より大にならないと膜体（ｆ）の透過流束が大とならず
、前記原水の線速度が前記所定値以下であると前記透過
流束が小となることが判明し、かくて透過流束を大にし
て分離濃縮効率を大にするためには原水のポンプ（Ｃ）
の吐出能力を大にして原水の線速度を大にする必要があ
り、従って分離濃縮装置の運転において大きなポンプ動
力を必要とする問題点がある。(3) Invention is MIL L, J-trying r! As a result of subsequent experiments on this conventional device, the inventor found that unless the linear velocity of the raw water on the outer surface of the membrane body (f) exceeds a predetermined value, the permeation flux of the membrane body (f) will decrease. It has been found that if the linear velocity of the raw water is below the predetermined value, the permeation flux becomes small. Thus, in order to increase the permeation flux and increase the separation and concentration efficiency, Raw water pump (C)
It is necessary to increase the discharge capacity of the raw water to increase the linear velocity of the raw water, and therefore there is a problem in that a large amount of pump power is required to operate the separation/concentration device.
本発明は大きなポンプ動力を必要とせずに分離濃縮効率
を大にした分離濃縮装置を提供することを目的とする。An object of the present invention is to provide a separation and concentration device that increases separation and concentration efficiency without requiring large pump power.
（４）問題点を解決するための手段
この目的を達成すべく本発明は一端に流入口を他端に流
出口を有する圧力容器内に、前記流入口から前記流出口
への原水の流線に直交するセラミック多孔体製の管状分
離濃縮膜体を設けたことを特徴とする。(4) Means for solving the problem In order to achieve this object, the present invention provides a pressure vessel having an inlet at one end and an outlet at the other end, and a flow line of raw water from the inlet to the outlet. A tubular separation/concentration membrane body made of a porous ceramic body is provided perpendicular to the membrane.
（５）作 用
原水の線速度が小であっても分子４濃縮膜体の透過流速
が大であり、かくて圧力容器へ原水を供給するポンプ動
力が小さくて済む。(5) Function Even if the linear velocity of the raw water is low, the permeation flow rate through the molecule 4 condensing membrane is high, and thus the pump power for supplying the raw water to the pressure vessel can be small.
（６）実施例
本発明装置の１実施例を第１図乃至第３図に従って説明
する。(6) Embodiment One embodiment of the apparatus of the present invention will be described with reference to FIGS. 1 to 3.
（１）は分離濃縮効率、（２）は該装置（１）の圧力容
器を示し、該圧力容器（２）は第１図の如く中間部が角
形筒状に形成されていると共にその両端部が１契形の筒
状に形成され、一端面に原水の流入口（３）を有すると
共に他端面に原水の流出口（４）を有しており、更に前
記圧力容器（２）の上面に等間隔に開口（５）を形成し
た。(1) shows the separation and concentration efficiency, and (2) shows the pressure vessel of the device (1). As shown in Fig. 1, the pressure vessel (2) is formed into a rectangular cylindrical shape at the middle part, and at both ends. is formed into a cylindrical shape, and has a raw water inlet (3) on one end face and a raw water outlet (4) on the other end face, and further has a raw water outlet (4) on the upper face of the pressure vessel (2). Openings (5) were formed at equal intervals.
（６）は分子濃縮膜体のユニットを示し、該ユニット（
６）は第３図の如く支持板（６ａ）に千鳥状に透孔（６
ｂ）・・・（６ｂ）を形成しこれら透孔（６ｂ）・・・
（６ｂ）にそれぞれ段着した先端が閉塞した管状の分ｔ
ａ儂縮膜体（６Ｃ）・・・（６Ｃ）と、前記支持板（６
ａ）上の頂板（６ｄ）と側板（６ｅ）とにより形成され
た透過液室（６ｆ）とからなり、これら各ユニット（６
）をその支持板（６ａ）において前記各開口（５）に嵌
着し、前記分離濃縮膜体（６ｃ）・・・（６ｃ）が前記
圧力容器（２）内において原水の流れに対して直交する
ようにした。(6) indicates a unit of a molecular concentration membrane body, and the unit (
6) is a support plate (6a) with through holes (6) arranged in a staggered manner as shown in
b)...(6b) are formed and these through holes (6b)...
(6b) A tubular portion t with a closed end is attached in each step.
a Shrinking membrane body (6C)... (6C) and the support plate (6
a) consists of a permeate chamber (6f) formed by an upper top plate (6d) and a side plate (6e);
) is fitted into each opening (5) on its support plate (6a), and the separation and concentration membrane body (6c)...(6c) is perpendicular to the flow of raw water in the pressure vessel (2). I decided to do so.
ここで前記各分ａ濃縮膜体（６Ｃ）は孔径０．３〜１０
、気孔率２５〜３５％のアルミナ等のセラミック焼
結体の単一の層状体或いは孔径０．３〜１０ 、気孔
率２５〜３０％のアルミナ等のセラミック焼結体の層状
支持体の表面に、微細なセラミック粉末をコーティング
して焼付けた焼結体からなる孔径０゜０１−１．気孔率
１０〜３０％の層即ちコーティング層を１０〜５００の
厚さで形成した複合層状体のセラミック多孔体からなる
。Here, each of the above-mentioned a concentration membrane bodies (6C) has a pore size of 0.3 to 10
, on the surface of a single layered ceramic sintered body such as alumina with a porosity of 25 to 35% or a layered support of a ceramic sintered body such as alumina with a pore size of 0.3 to 10% and a porosity of 25 to 30%. , a sintered body coated with fine ceramic powder and baked, with a pore diameter of 0°01-1. It consists of a composite layered ceramic porous body in which a layer with a porosity of 10 to 30%, that is, a coating layer, is formed with a thickness of 10 to 500%.
以上のように構成された分離濃縮装置（１）は第４図の
如くスクリーニングした原水のばっ気槽（７）の流出口
から該ばっ気槽（７）に戻る環流管路（８）に介在した
。尚１図中、（９）はポンプ、（１０ａ）（１０ｂ）は
流量計、（１１）はｒｌ’ニーｈ斗／ｌ０Ａ）ｌｊｌｊ
ＬＩＩｌｊ１４ ／１ＱＬＴｈ＋Ｊ）六ｆｆｉ調
整弁、（１３）は前記支持板（６ａ）に形成した透過液
の流出口、（１４）はこれら流出口（１３）・・・（１
３）からの透過液の流出管、（１５）は該透過液の貯槽
を示す。The separation/concentration device (1) configured as above is interposed in a reflux pipe (8) returning from the outlet of the aeration tank (7) of the screened raw water to the aeration tank (7) as shown in Fig. 4. did. In Figure 1, (9) is the pump, (10a) and (10b) are the flow meters, and (11) is the rl'kneehto/l0A)ljlj
LIIlj14 /1QLTh+J)6ffi adjustment valve, (13) is the permeate outlet formed in the support plate (6a), (14) is the outlet (13)...(1
3), and (15) indicates a storage tank for the permeate.
次に上記装置の作動について説明する。Next, the operation of the above device will be explained.
ばっ気槽（７）から原水をポンプ（９）により管路（８
）を経て圧力容器（２）内にその流入口（３）から流出
口（４）に向けて流すと、この流′れに直交する各分ａ
ｇｌｌｉｉ膜体（６Ｃ）においてそ・の外側の原水は該
膜体（６ｃ）により活性汚泥が分離され、該１１！２体
（６Ｃ）を透過した透過液は該膜体（６ｃ）内を流れて
流出管（１４）を経て貯槽（１５）に貯められる。又活
性汚泥の濃縮液は管路（８）を経てばっ気槽（７）に戻
る。Raw water is pumped from the aeration tank (7) to the pipe (8) by the pump (9).
) into the pressure vessel (2) from its inlet (3) to its outlet (4), each part perpendicular to this flow a
Activated sludge is separated from the raw water outside the gllii membrane body (6C) by the membrane body (6c), and the permeate that has passed through the 11!2 body (6C) flows inside the membrane body (6c). and is stored in a storage tank (15) via an outflow pipe (14). The activated sludge concentrate returns to the aeration tank (7) via the pipe (8).
ここで前記分ａ濃縮膜体（６Ｃ）の分ｇｉ濠縮の作用は
下記のように行われる。Here, the action of the gi condensation of the a-concentration membrane body (6C) is performed as follows.
前記単一層状体或いは複合層状体の１方の表面に活性汚
泥の混合水即ち原水を加圧して流すとこれに含まれる活
性汚泥コロイド物質が該表面に捕捉され、一定時間経過
後詰表面上にコロイド物質が堆積しダイナミック膜が形
成される。その後も原水を加圧して流し続けると該ダイ
ナミック膜が自己排除型のダイナミック膜として大腸菌
を含む活性汚泥を分離濃縮し、他方の表面からはこれら
活性汚泥を除去した透過液が得られる。When activated sludge mixed water, that is raw water, is flowed under pressure on one surface of the single layered body or composite layered body, the activated sludge colloidal substances contained therein are captured on the surface, and after a certain period of time have passed, they are deposited on the packing surface. Colloidal material is deposited to form a dynamic film. After that, when the raw water continues to flow under pressure, the dynamic membrane acts as a self-exclusion type dynamic membrane, separating and concentrating activated sludge containing E. coli, and a permeate from which the activated sludge has been removed is obtained from the other surface.
次に、発明者は前記原水として汚泥濃度的４０００ｍｇ
／ ｌで温度約３５°Ｃのものを用意し、該原水を本発
明の前記実施例装置と前記従来の装置にそれぞれ流し、
３時間経過後における原水の線速度と膜体の透過流束の
関係を求めたところ第５図のグラフのような実験結果が
得られた。Next, the inventor obtained 4000 mg of sludge concentration as the raw water.
/l at a temperature of about 35°C, and flowing the raw water into the apparatus according to the embodiment of the present invention and the conventional apparatus, respectively.
When the relationship between the linear velocity of the raw water and the permeation flux of the membrane body after 3 hours was determined, the experimental results shown in the graph of FIG. 5 were obtained.
ここで、Ａ−Ｃは本発明装置の実験結果でＡは膜体間の
ピッチがｌｓｍの場合、Ｂは同ピツチが２ａ膠の場合、
Ｃは同ピツチが３■の場合であり、又りは従来装置の場
合である。Here, A-C are the experimental results of the device of the present invention, A is when the pitch between the membrane bodies is lsm, B is when the same pitch is 2a glue,
C is the case where the same pitch is 3cm, or the case of the conventional device.
この第５図のグラフより本発明装置は従来装置と比べて
線速度が比較的小のときにおいても透過流速が大となり
、従って圧力容器（２）に原水を供給するポンプ（９）
の動力が小さくてすむ。The graph in FIG. 5 shows that the device of the present invention has a large permeation flow rate even when the linear velocity is relatively small compared to the conventional device, and therefore the pump (9) that supplies raw water to the pressure vessel (2)
The power required is small.
（７）発明の効果
このように本発明によると圧力容器内においてセラミッ
ク多孔体製の管状分離１Ｍ縮膜体を原水の流線に直交さ
せたので、従来の装置と比べて該原水の線速度が小さく
でも前記膜体の透過流束が大であり、かくて前記圧力容
器へ原−水を供給するポンプの動力が小さくて済み、従
って運転コストの低減が図れる効果を有する。(7) Effects of the invention As described above, according to the present invention, the tubular separator 1M membrane shrinking body made of a porous ceramic material is arranged perpendicularly to the streamline of the raw water in the pressure vessel, so that the linear velocity of the raw water is higher than that of the conventional device. Even if the amount of water is small, the permeation flux of the membrane is large, and thus the power of the pump for supplying raw water to the pressure vessel is small, which has the effect of reducing operating costs.
：５１図は本発明装置の１実施例の１部を截除した斜視
図、第２図は分離濃縮膜体ユニットの断面図、第３図は
その■−ｍ線截線面断面図４図は配管系統図、第５図は
実験結果のグラフ、第６図は従来装置の配管系統図、第
７図は該装置の正面図、第８図はそのτ−葭線截断面図
である。
（１）・・・分離濃縮装置 （２）・・・圧力容器（３
）・・・流入口 （４）・・・流出口（６Ｃ）・
・・管状分＃Ｓ縮膜体
第３図
６ｂ ６ａ
□Figure 51 is a partially cutaway perspective view of one embodiment of the device of the present invention, Figure 2 is a cross-sectional view of the separation and concentration membrane unit, and Figure 3 is a cross-sectional view taken along the line ■-m. is a piping system diagram, FIG. 5 is a graph of experimental results, FIG. 6 is a piping system diagram of a conventional device, FIG. 7 is a front view of the device, and FIG. 8 is a cross-sectional view taken along the τ-line. (1)... Separation and concentration equipment (2)... Pressure vessel (3
)...Inlet (4)...Outlet (6C)
・・Tubular part #S membrane shrinkage body Fig. 3 6b 6a □
Claims (2)
に、前記流入口から前記流出口への原水の流線に直交す
るセラミック多孔体製の管状分離濃縮膜体を設けたこと
を特徴とする活性汚泥の分離濃縮装置(1) In a pressure vessel having an inlet at one end and an outlet at the other end, a tubular separation and concentration membrane body made of a porous ceramic body is provided which is perpendicular to the flow line of raw water from the inlet to the outlet. Activated sludge separation and concentration equipment featuring
特徴とする特許請求の範囲第１項記載の活性汚泥の分離
濃縮装置(2) The activated sludge separation and concentration apparatus according to claim 1, characterized in that the tubular separation and concentration membrane bodies are arranged in a staggered manner.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61047923A JPS62204812A (en) | 1986-03-05 | 1986-03-05 | Separation and concentration device for activated sludge |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61047923A JPS62204812A (en) | 1986-03-05 | 1986-03-05 | Separation and concentration device for activated sludge |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS62204812A true JPS62204812A (en) | 1987-09-09 |
Family
ID=12788889
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61047923A Pending JPS62204812A (en) | 1986-03-05 | 1986-03-05 | Separation and concentration device for activated sludge |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS62204812A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0220999U (en) * | 1988-07-25 | 1990-02-13 | ||
| JPH057886A (en) * | 1990-11-30 | 1993-01-19 | Ebara Infilco Co Ltd | Method for biological treatment integrated with solid-liquid separation and device therefor |
| CN103663881A (en) * | 2013-12-19 | 2014-03-26 | 天津英利新能源有限公司 | System for treating photovoltaic sewage and sludge recycling device for system |
| JP2019013874A (en) * | 2017-07-05 | 2019-01-31 | 株式会社アクト | Sludge volume reduction method, sludge volume reduction device and waste water purification system |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS50150681A (en) * | 1974-05-23 | 1975-12-03 | ||
| JPS5586509A (en) * | 1978-12-26 | 1980-06-30 | Nec Corp | Filter housing for pure water filtration |
| JPS5589390A (en) * | 1978-12-27 | 1980-07-05 | Nitto Electric Ind Co Ltd | Waste oil purifier |
-
1986
- 1986-03-05 JP JP61047923A patent/JPS62204812A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS50150681A (en) * | 1974-05-23 | 1975-12-03 | ||
| JPS5586509A (en) * | 1978-12-26 | 1980-06-30 | Nec Corp | Filter housing for pure water filtration |
| JPS5589390A (en) * | 1978-12-27 | 1980-07-05 | Nitto Electric Ind Co Ltd | Waste oil purifier |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0220999U (en) * | 1988-07-25 | 1990-02-13 | ||
| JPH0534800Y2 (en) * | 1988-07-25 | 1993-09-02 | ||
| JPH057886A (en) * | 1990-11-30 | 1993-01-19 | Ebara Infilco Co Ltd | Method for biological treatment integrated with solid-liquid separation and device therefor |
| CN103663881A (en) * | 2013-12-19 | 2014-03-26 | 天津英利新能源有限公司 | System for treating photovoltaic sewage and sludge recycling device for system |
| JP2019013874A (en) * | 2017-07-05 | 2019-01-31 | 株式会社アクト | Sludge volume reduction method, sludge volume reduction device and waste water purification system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4451369A (en) | Fluid separation apparatus | |
| US3774771A (en) | Reverse osmosis module | |
| JPS6082B2 (en) | Thin membrane filtration device | |
| US5089122A (en) | Device for the separation of fluid mixtures | |
| EP0307047A1 (en) | Membrane module for hyperfiltration or ultrafiltration of contaminating liquid flows | |
| US3400825A (en) | Desalination cell with osmotic membrane element | |
| JP2004202480A (en) | Membrane separation apparatus and membrane separation method | |
| JP3098600B2 (en) | Spiral type separation membrane module | |
| EP0493869A1 (en) | Apparatus for treating water | |
| JP2009213984A (en) | Separation membrane module for filtration, and filtration apparatus using the same | |
| JP3230490B2 (en) | Spiral reverse osmosis membrane element and separation device using the same | |
| EP0354797A2 (en) | Degassing device | |
| JPS62204812A (en) | Separation and concentration device for activated sludge | |
| JPH0683778B2 (en) | Fluid component diffusion controller | |
| US3698559A (en) | Reverse osmosis module suitable for food processing | |
| JPH06335623A (en) | Deaerating film and deaerating method | |
| JPS6241764B2 (en) | ||
| US5985151A (en) | Method and apparatus of membrane separation | |
| JPH03249907A (en) | Spiral type deaerating element and method for using this element | |
| JP2666200B2 (en) | Water purification equipment | |
| GB2277885A (en) | Ceramic filter and membrane | |
| JPS61185372A (en) | Apparatus for treating excretion sewage | |
| JPH0474584A (en) | Treatment of waste water | |
| JP2000093729A (en) | Gas separation module | |
| KR20140087416A (en) | Hollow fiber membrane module |