JPH02227122A - Treatment by membrane - Google Patents
Treatment by membraneInfo
- Publication number
- JPH02227122A JPH02227122A JP4614689A JP4614689A JPH02227122A JP H02227122 A JPH02227122 A JP H02227122A JP 4614689 A JP4614689 A JP 4614689A JP 4614689 A JP4614689 A JP 4614689A JP H02227122 A JPH02227122 A JP H02227122A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- liquid
- raw liquid
- phase flow
- membrane
- 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.)
- Granted
Links
- 239000012528 membrane Substances 0.000 title claims abstract description 41
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 239000002245 particle Substances 0.000 claims abstract description 22
- 239000007787 solid Substances 0.000 claims abstract description 18
- 239000011550 stock solution Substances 0.000 claims description 27
- 238000000034 method Methods 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 6
- 239000012530 fluid Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000009295 crossflow filtration Methods 0.000 claims description 2
- 238000003672 processing method Methods 0.000 claims 1
- 238000000746 purification Methods 0.000 claims 1
- 238000000926 separation method Methods 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 19
- 239000012141 concentrate Substances 0.000 abstract 2
- 239000011343 solid material Substances 0.000 abstract 2
- 230000001174 ascending effect Effects 0.000 abstract 1
- 230000001105 regulatory effect Effects 0.000 abstract 1
- 230000004907 flux Effects 0.000 description 15
- 230000005514 two-phase flow Effects 0.000 description 6
- 239000011148 porous material Substances 0.000 description 3
- 239000008247 solid mixture Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 2
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 2
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000003456 ion exchange resin Substances 0.000 description 2
- 229920003303 ion-exchange polymer Polymers 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 238000005273 aeration Methods 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 239000002504 physiological saline solution Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
（ａ業上の利用分野）
本発明は原液を液体、気体及び固体を混合した三相流と
して膜処理する方法に関する。DETAILED DESCRIPTION OF THE INVENTION (Field of Industrial Application) The present invention relates to a method for membrane processing a stock solution as a three-phase flow containing a mixture of liquid, gas, and solid.
（従来の技術）
排水や下水を処理する嫌気性菌体をリアクタ内に高濃度
に保持するためや、食品工業における溶液の分離、濃縮
等を行う膜処理方法として本出願人は先に特開昭６３−
１０４６１０号として、原液を気・液・固混合の三相流
として膜モジユール内に供給し、クロスフロー濾過方式
によって処理する方法を提案している。(Prior art) The present applicant previously published a patent application as a membrane treatment method for maintaining high concentration of anaerobic bacteria in a reactor for treating wastewater and sewage, and for separating and concentrating solutions in the food industry. 1986-
No. 104610 proposes a method in which a stock solution is supplied into a membrane module as a three-phase flow of a mixture of gas, liquid, and solid, and processed by a cross-flow filtration method.
（発明が解決しようとする課題）
上述した気・液・固混合の三相流とすれば、°気液二相
流に比べ乱流促進効果は更に高くなり、膜表面に付着し
た微粒子や溶質成分からなるゲル層は二相流の場合より
も有効に掻き落され、透過流束が大きくなることが期待
される。しかしながら、膜表面のゲル層を完全に除去し
てしまうと、却って膜内に微粒子が侵入して目詰まりを
起し、透過流束が低下する結果となる。したがって固体
としての微粒子の添加割合に関しては一定の範囲とすべ
きである。(Problem to be solved by the invention) If the three-phase flow of gas, liquid, and solid mixture is used as described above, the effect of promoting turbulence will be even higher than that of gas-liquid two-phase flow, and the fine particles and solutes attached to the membrane surface will be more effective. It is expected that the gel layer consisting of the components will be scraped off more effectively than in the case of two-phase flow, and that the permeation flux will be larger. However, if the gel layer on the membrane surface is completely removed, fine particles will instead enter the membrane and cause clogging, resulting in a decrease in permeation flux. Therefore, the proportion of solid particles to be added should be within a certain range.
一方、気・液・固三相流では気・液二相流と同様に、各
相の分布が不均一となった複雑な流れを呈するため、液
単相流に比べて常に透過流束が大きいとは限らないこと
が実験の結果判明し、特に膜モジュールを多数本の細管
状膜にて構成した場合には上記の傾向が強くなった。On the other hand, gas-liquid-solid three-phase flow presents a complex flow with uneven distribution of each phase, similar to gas-liquid two-phase flow, so the permeation flux is always lower than liquid single-phase flow. As a result of experiments, it has been found that the size is not necessarily large, and the above tendency becomes particularly strong when the membrane module is composed of a large number of tubular membranes.
（課題を解決するための手段）
上記課題を解決すべく本発明は、原液を三相流として自
然循環させるために供給するガス量をＱ ｇ ［Ｎｍ’
・■Ｉｎ−’］ 、最大循環液流量を与えるガス量をＱ
’ ｇ ［Ｎｍ３１ｉｎ−’］ ％小粒子の添加割合を
ｘ ［ｖｏｌ駒とした場合、これらがＱ’ ｇ≦Ｑｇ（
１＋ｘ）≦フＱ’ ｇとなるようにした。(Means for Solving the Problems) In order to solve the above problems, the present invention provides that the amount of gas to be supplied in order to naturally circulate the stock solution as a three-phase flow is Q g [Nm'
・■In-'], Q is the gas amount that gives the maximum circulating fluid flow rate.
'g[Nm31in-']%If the addition ratio of small particles is x [vol piece, then these are Q'g≦Qg(
1+x)≦FQ'g.
（作用）
上記の条件を満たすように原液を三相流として膜モジュ
ールに供給すれば、二相流よりも透過流束を大きく、ま
た消費動力も低く抑えることができる。(Function) If the stock solution is supplied to the membrane module as a three-phase flow so as to satisfy the above conditions, the permeation flux can be made larger than in the case of a two-phase flow, and the power consumption can also be kept low.
（実施例） 以下に本発明の実施例を添付図面に基づいて説明する。(Example) Embodiments of the present invention will be described below based on the accompanying drawings.
第１図は本発明方法を実施する膜処理装置の全体図であ
り、原液１を満たした原液タンク２は攪拌装置３及び温
度調節装置４を備え、原液タンク２内の原液１をポンプ
５によって供給管６を介してセパレータフに供給するよ
うにしている。FIG. 1 is an overall view of a membrane treatment apparatus for carrying out the method of the present invention. A stock solution tank 2 filled with stock solution 1 is equipped with a stirring device 3 and a temperature control device 4, and the stock solution 1 in the stock solution tank 2 is pumped by a pump 5. It is supplied to the separator trough via a supply pipe 6.
セパレータ７は隔壁８によって２つの室に区画され、一
方の室には供給管６が臨み、他方の室にはイオン交換樹
脂粒、砂等の小粒子固形物９が貯溜され、更にセパレー
タ７の他方の室には小粒子固形物９の通過を阻止するス
クリーン１０を設け、他方の室と原液タンク２とを戻り
管１１にてつないでいる。The separator 7 is divided into two chambers by a partition wall 8, one chamber faces the supply pipe 6, and the other chamber stores small particle solids 9 such as ion exchange resin particles and sand. The other chamber is provided with a screen 10 for preventing the passage of small solid particles 9, and the other chamber and the stock solution tank 2 are connected by a return pipe 11.
また、セパレータからは下方に降下管１２を導出し、降
下管１２の途中には電磁流量計１３を設けるとともに、
降下管１２の下端をＵ字状に湾曲して上昇管１４に接続
し、この上昇管１４の途中に全網製の散気筒を備えた気
液混合器１５を設け、この気液混合器１５にブロワ１６
からガス（空気）を供給し、供給ガス量は配管の途中に
設けたガス流量計１７で測定するようにしている。In addition, a downcomer pipe 12 is guided downward from the separator, and an electromagnetic flowmeter 13 is provided in the middle of the downcomer pipe 12.
The lower end of the downcomer pipe 12 is curved into a U-shape and connected to the riser pipe 14, and a gas-liquid mixer 15 equipped with a full-mesh aeration tube is provided in the middle of the riser pipe 14. blower 16
Gas (air) is supplied from the piping, and the amount of supplied gas is measured by a gas flow meter 17 installed in the middle of the piping.
また気液混合器１５の上部にはスタティックミキサー１
８を設け、このスタティックミキサー１８の上方に５連
の膜モジュール１９・・・を垂直方向に接続している。Additionally, a static mixer 1 is placed above the gas-liquid mixer 15.
8 is provided, and five membrane modules 19 are vertically connected above the static mixer 18.
各膜モジユール１９内には管状透過膜を配置し、管状透
過膜の内側通路と前記上昇管１４及びセパレータ７への
戻し管２０とをつなぎ、管状透過膜の外側流路と透過水
の取出し管２１とをつなぎ、取出し管２１の先端は逆洗
バッファ２２内に臨み、この逆洗バッファ２２内にはコ
ンプレッサ２３によって加圧空気を供給し、空気圧によ
ってバッファ２２内の透過水を電子天秤２４上に載置し
た集水タンク２５又は切換用減圧タンク２６に送り込む
ようにしている。A tubular permeable membrane is arranged in each membrane module 19, and the inner passage of the tubular permeable membrane is connected to the riser pipe 14 and the return pipe 20 to the separator 7, and the outer passage of the tubular permeable membrane and the permeated water take-out pipe are connected. 21, and the tip of the extraction pipe 21 faces into the backwash buffer 22. Pressurized air is supplied into the backwash buffer 22 by a compressor 23, and the permeated water in the buffer 22 is transferred onto the electronic balance 24 by the air pressure. The water is sent to a water collection tank 25 or a switching decompression tank 26 mounted on the water tank 25 or the decompression tank 26 for switching.
集水タンク２５及び切替用減圧タンク２６には膜間差圧
を与える排気ポンプ２７が接続され、集水タンク２５に
は液面計２８を付設している。而して、集水タンク２５
の重量増加速度を電子天秤２４にて計測することで透過
流束を求めることができ、また集水タンク２５内に所定
量の透過水が溜ったことを液面計２８によって感知した
ならば、自動的に切替用減圧タンク２６への捕集に切替
わり、この間に集水タンク２５内の減圧状態は解除され
て大気圧となり、集水タンク２５内の透過水は原液タン
ク２へ戻される。同様にして切替用減圧タンク２６内の
透過水も原液タンク２に戻され、装置全体としては前循
環濾過方式を採用している。An exhaust pump 27 that provides a transmembrane pressure difference is connected to the water collection tank 25 and the switching reduced pressure tank 26, and a liquid level gauge 28 is attached to the water collection tank 25. Therefore, water collection tank 25
The permeation flux can be determined by measuring the weight increase rate of the water with the electronic balance 24, and if the liquid level gauge 28 detects that a predetermined amount of permeated water has accumulated in the water collection tank 25, The collection is automatically switched to the switching reduced pressure tank 26, and during this time, the reduced pressure state in the water collection tank 25 is released and becomes atmospheric pressure, and the permeated water in the water collection tank 25 is returned to the stock solution tank 2. Similarly, the permeated water in the switching reduced pressure tank 26 is also returned to the stock solution tank 2, and the entire device employs a pre-circulation filtration system.
更に、降下管１２と上昇管１４とをつなぐＵ字状部につ
いては着脱可能とし、液単相流として膜モジユール１９
内へ原液を供給する場合にはこの部分に循環ポンプ２９
を接続するようにしている。Furthermore, the U-shaped part connecting the downcomer pipe 12 and the riser pipe 14 is made removable, so that the membrane module 19 can be used as a liquid single-phase flow.
When supplying the stock solution to the inside, a circulation pump 29 is installed in this part.
I am trying to connect.
以上において、原液タンク２からポンプ５の駆動によつ
てセパレータ７内に供給された原液１は、セパレータ７
内において小粒子固形物９が添加され、この小粒子固形
物９が混入した原液１は降下管１２内を通って下降し、
上昇管１４に入り、気液混合器１５の部分でガスが吹込
まれる。In the above, the stock solution 1 supplied from the stock solution tank 2 into the separator 7 by driving the pump 5 is
Small particle solids 9 are added therein, and the stock solution 1 mixed with the small particle solids 9 descends through the downcomer pipe 12.
The gas enters the riser pipe 14 and is blown into the gas-liquid mixer 15.
そして、原液１内に吹込まれたガスは流路の中央部を上
昇し、原液１は流路の外周部つまり管状透過膜の内側面
に沿って上昇し、更に原液１中に添加されている小粒子
固形物９は原液１とともに流動する。その結果、管状透
過膜の内側面に付着しているスケール（ゲル層）に小粒
子固形物９が接触し、スケールが掻き落とされる。Then, the gas blown into the stock solution 1 rises in the center of the channel, and the stock solution 1 rises along the outer periphery of the channel, that is, the inner surface of the tubular permeable membrane, and is further added to the stock solution 1. The small particle solids 9 flow together with the stock solution 1. As a result, the small solid particles 9 come into contact with the scale (gel layer) adhering to the inner surface of the tubular permeable membrane, and the scale is scraped off.
一方、透通膜内に流入した原液１は透過水と濃縮液に分
離され、透過水は取り出し管２１によて取り出され、濃
縮液は戻し管２０を介してセパレータ７を介して原液タ
ンク２に戻される。On the other hand, the stock solution 1 that has flowed into the permeable membrane is separated into permeate water and concentrated solution. will be returned to.
ここで気液混合器１５からは連続的にガスが原液１中に
吹き込まれるため、序章管１４及び膜モジユール１９内
の流路にはガスが存在し、みかけの比重が低下し、降下
管１２内の原液との水頭差によって自然に循環流が生じ
ることとなる。Here, since gas is continuously blown into the raw liquid 1 from the gas-liquid mixer 15, gas exists in the flow paths in the introductory pipe 14 and the membrane module 19, and the apparent specific gravity decreases, causing the downcomer pipe 12 Circulating flow will naturally occur due to the difference in water head with the undiluted solution inside.
第２図は上述した構成の膜処理装置を用いて減車相流と
した場合と気・液・固混合三相流とした場合の透過流束
とブロワの消費動力との関係を示すグラフである。FIG. 2 is a graph showing the relationship between the permeation flux and the power consumption of the blower when the membrane treatment device having the above-mentioned configuration is used to generate a reduced phase flow and when a gas/liquid/solid mixed three-phase flow is generated. .
尚、第２図の結果を得るにあたっての具体的な条件は以
下の通りである。The specific conditions for obtaining the results shown in FIG. 2 are as follows.
原 液： ０．９％生理食塩水に乾燥パン酵母を分散さ
せた懸濁液
パン酵母濃度：１０Ｋｇ・■−３
温 度＝２５℃
透過膜の寸法：外径５．２ｍｍ ｓ内径３．８ｍｍ 、
長さ５００ｍ■のセラミック膜を２００本／そジュール
透過膜の構造：孔径０．５μ履の均質膜又は０．２μ諺
の非対称膜
小粒子：平均粒径Ｑ、８ａｍのイオン交換樹脂小粒子の
添加割合： ５．０ｖｏｌ零以下膜間圧差：６０ｋｌ）
ａ
第２図からは透過流束Ｊが０．７［ｎ＋３・「２・ｄ−
１１未満であると、減車相流とした方が消費動力が小さ
くなり、透過流束が２．０［■３・１１−２・４−１］
を超えると単相流・三相流にかかわらず、消費動力が大
幅に増加することが分かる。Stock solution: Suspension of dried baker's yeast dispersed in 0.9% physiological saline Baker's yeast concentration: 10Kg・■-3 Temperature = 25℃ Dimensions of permeable membrane: Outer diameter 5.2mm s Inner diameter 3.8mm ,
200 ceramic membranes with a length of 500 m / 2 joules Structure of permeable membrane: Homogeneous membrane with pore size of 0.5 μm or asymmetric membrane with pore size of 0.2 μm Small particles: Small particles of ion exchange resin with average particle size Q, 8 am Addition ratio: 5.0vol (below zero transmembrane pressure difference: 60kl)
a From Figure 2, the permeation flux J is 0.7[n+3・``2・d−
If it is less than 11, the power consumption will be smaller if the vehicle phase flow is reduced, and the permeation flux will be 2.0 [■3・11-2・4-1]
It can be seen that when the value exceeds , the power consumption increases significantly regardless of single-phase flow or three-phase flow.
したがって、透過流束は気・液・固三相流とする場合は
０．７〜２．０［ｍ’・■−２・ｄ−１］の範囲とすべ
きである。Therefore, the permeation flux should be in the range of 0.7 to 2.0 [m'·■-2·d-1] in the case of a gas-liquid-solid three-phase flow.
ところで、本発明にあっては前記したように気・液・固
三相流として自然循環させるのは、専ら気液混合器１５
から供給されるガスに依存している。そこで、供給ガス
量Ｑｇと透過流束Ｊとの関係を示したのが第３図（Ａ）
である。By the way, in the present invention, as described above, the natural circulation as a three-phase flow of gas, liquid, and solid is exclusively carried out in the gas-liquid mixer 15.
depend on gas supplied by Therefore, Figure 3 (A) shows the relationship between the supply gas amount Qg and the permeation flux J.
It is.
小粒子を殆ど添加しない二相流に近い状態において透過
流束Ｊが０．７〜２．０〔■３・「２・ｄ−１１となる
のは、供給ガス量Ｑｇが０．０６〜０．３５［Ｎｍ’・
５ｉｎ−’］の範囲であることが分る。しかしながら供
給ガス量Ｑｇと透過流束Ｊとの関係は膜モジュール１９
・・・の配列や膜の孔径によって一義的に定まるもので
はない。In a state close to a two-phase flow with almost no addition of small particles, the permeation flux J becomes 0.7 to 2.0 [■3. .35[Nm'・
5in-']. However, the relationship between the supply gas amount Qg and the permeation flux J is
It is not uniquely determined by the arrangement of ... or the pore size of the membrane.
そこで供給ガス量Ｑｇと循環流量ＱＪ２とが一定の関係
があることに看目し、これを第３図（Ｂ）で示した。即
ち、第３図（Ｂ）に示すように供給ガス量Ｑｇを最大循
環流量Ｑｇを与える供給ガス量Ｑ’ ｇの１〜７倍の範
囲とすることで減車相流よりも消費動力の面で有利な気
・液・固混合の三相流とすることができる。Therefore, it was noted that there is a certain relationship between the supply gas amount Qg and the circulating flow rate QJ2, and this is shown in FIG. 3(B). That is, as shown in Fig. 3 (B), by setting the supply gas amount Qg to a range of 1 to 7 times the supply gas amount Q'g that provides the maximum circulation flow rate Qg, it is possible to improve the power consumption compared to the reduced vehicle phase flow. An advantageous three-phase flow of gas/liquid/solid mixture can be achieved.
一方、第３図（Ａ）からも明らかなように、小粒子の添
加割合Ｘ （ｖｏｌｌ）によって気・液・固三相流が気
・液二相流よりも有利になる場合とならない場合がある
ことが分る。即ち、添加割合を５．０［ｍｏｌ＄１］と
した場合には供給ガス量Ｑｇは０．０７ ［Ｎｍ”・ｌ
ｌ１ｎ−′１以下とし、添加割合を２．５ ［ｖｏｌｋ
ｌ とした場合には供給ガス量Ｑｇは０．１［Ｎ＋ｓ３
・ｍ１ｎ−’］以下としないと有利にならない。つまり
小粒子の添加割合が多くなる程、供給ガス量Ｑｇを少な
くしなければならない。On the other hand, as is clear from Figure 3 (A), depending on the addition ratio of small particles I understand something. That is, when the addition ratio is 5.0 [mol$1], the supplied gas amount Qg is 0.07 [Nm"・l
l1n-'1 or less, and the addition ratio is 2.5 [volk
l, the supplied gas amount Qg is 0.1[N+s3
・m1n-'] or less, it will not be advantageous. In other words, the larger the proportion of small particles added, the smaller the supplied gas amount Qg must be.
以上をまとめると、気・液・固混合の三相流として膜モ
ジエール１９内に原液を供給する場合は、Ｑ’ ｇ≦
Ｑ（１＋Ｘ）≦フＱ゛の条件を満たすように運転すべき
である。To summarize the above, when supplying the stock solution into the membrane module 19 as a three-phase flow of gas, liquid, and solid mixture, Q' g≦
It should be operated so that the condition Q(1+X)≦FQ' is satisfied.
（発明の効果）
以上に説明した如く本発明によれば、原液を気・液・固
三相流として膜モジュールに送り込んで処理する際に、
供給ガス量及び小粒子の添加割合を所定範囲にすること
で、膜モジュールのランニングコストの約半分を占める
と言われる消費動力を減車相流及び気液二相流に比べて
大幅に低減することができる。(Effects of the Invention) As explained above, according to the present invention, when the stock solution is sent to the membrane module as a gas-liquid-solid three-phase flow for treatment,
By adjusting the amount of gas supplied and the addition ratio of small particles within a specified range, the power consumption, which is said to account for about half of the running cost of a membrane module, can be significantly reduced compared to reduced-vehicle phase flow and gas-liquid two-phase flow. Can be done.
第１図は本発明方法を実施する膜処理装置の全体図、第
２図は透過流束と消費電力との関係を示すグラフ、第３
図（Ａ）及び（Ｂ）はそれぞれ供給ガス量と透過流束及
び循環液流量との関係を示すグラフである。
尚、図面中、１は原液、２は原液タンク２．７はセパレ
ータ、９は小粒子、１２は降下管、１４は上昇管、１５
は気液混合器、１９は膜モジュールである。Fig. 1 is an overall view of a membrane treatment apparatus for carrying out the method of the present invention, Fig. 2 is a graph showing the relationship between permeation flux and power consumption, and Fig. 3 is a graph showing the relationship between permeation flux and power consumption.
Figures (A) and (B) are graphs showing the relationship between the supply gas amount, permeation flux, and circulating fluid flow rate, respectively. In addition, in the drawing, 1 is the stock solution, 2 is the stock solution tank 2. 7 is the separator, 9 is the small particle, 12 is the downcomer pipe, 14 is the riser pipe, 15
1 is a gas-liquid mixer, and 19 is a membrane module.
Claims (1)
体を混合した三相流として供給し、クロスフロー濾過方
式によって精製、濃縮或は分離を行うようにした膜処理
方法において、前記原液を三相流として自然循環させる
ために供給するガス量をＱｇ［Ｎｍ＾３・ｍｉｎ＾−＾
１］、最大循環液流量を与えるガス量をＱ’ｇ［Ｎｍ＾
３・ｍｉｎ＾−＾１］、固体としての小粒子の添加割合
をｘ［ｖｏｌ％］とした場合、これらは以下の関係を満
たすようにしたことを特徴とする膜処理方法。 Ｑ’ｇ≦Ｑｇ（１＋ｘ）≦７Ｑ’ｇ[Claims] A membrane treatment method in which a stock solution is supplied as a three-phase flow containing a mixture of liquid, gas, and solid to a membrane module equipped with a permeable membrane, and purification, concentration, or separation is performed by a cross-flow filtration method. In order to naturally circulate the stock solution as a three-phase flow, the amount of gas supplied is Qg[Nm^3・min^-^
1], the gas amount that gives the maximum circulating fluid flow rate is Q'g[Nm^
3.min^-^1], and the addition ratio of small particles as a solid is x [vol%], the membrane processing method is characterized in that these satisfy the following relationship. Q'g≦Qg(1+x)≦7Q'g
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1046146A JPH0751216B2 (en) | 1989-02-27 | 1989-02-27 | Membrane treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1046146A JPH0751216B2 (en) | 1989-02-27 | 1989-02-27 | Membrane treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02227122A true JPH02227122A (en) | 1990-09-10 |
| JPH0751216B2 JPH0751216B2 (en) | 1995-06-05 |
Family
ID=12738830
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1046146A Expired - Fee Related JPH0751216B2 (en) | 1989-02-27 | 1989-02-27 | Membrane treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0751216B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07251043A (en) * | 1994-01-28 | 1995-10-03 | Toto Ltd | Filtering method and filter device |
| JPH0824594A (en) * | 1994-07-22 | 1996-01-30 | Toto Ltd | Operation of filter |
| NL1018870C2 (en) * | 2001-09-03 | 2003-03-05 | Waterleiding Mij Overijssel N | Effluent purification process, comprises recirculating mixture of additive and pre treated effluent along tubular nanofiltration or reverse osmosis membrane |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63104610A (en) * | 1986-10-20 | 1988-05-10 | Akua Runesansu Gijutsu Kenkyu Kumiai | Method and device for treating membrane |
-
1989
- 1989-02-27 JP JP1046146A patent/JPH0751216B2/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63104610A (en) * | 1986-10-20 | 1988-05-10 | Akua Runesansu Gijutsu Kenkyu Kumiai | Method and device for treating membrane |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07251043A (en) * | 1994-01-28 | 1995-10-03 | Toto Ltd | Filtering method and filter device |
| JPH0824594A (en) * | 1994-07-22 | 1996-01-30 | Toto Ltd | Operation of filter |
| NL1018870C2 (en) * | 2001-09-03 | 2003-03-05 | Waterleiding Mij Overijssel N | Effluent purification process, comprises recirculating mixture of additive and pre treated effluent along tubular nanofiltration or reverse osmosis membrane |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0751216B2 (en) | 1995-06-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4992216A (en) | Method for producing ozone-containing water | |
| US3711072A (en) | Apparatus for oxygenation of liquids | |
| WO2008053700A1 (en) | Method of desalting, apparatus for desalting, and bubble generator | |
| JP2007000699A (en) | Production method of nitrogen gas-dissolved water | |
| US20220234930A1 (en) | Method for Purifying Contaminated Water | |
| US3855124A (en) | Process and apparatus for the purification of an aqueous waste stream from a silicone-polymer producing plant | |
| CN207877300U (en) | A kind of ultra-pure water decarburization/device for deoxidizing system based on membrane contactor | |
| Lazaridis et al. | A hybrid MF process based on flotation | |
| JPH05317605A (en) | Membrane vacuum deaerating method and device therefor | |
| JPS5819325B2 (en) | Biseibutsu koubunshi mataha bisainakotai o ganyuusuru ekitai o lokasurutameno hohou oyobi souchi | |
| JPH02227122A (en) | Treatment by membrane | |
| JPS63104610A (en) | Method and device for treating membrane | |
| US20020038782A1 (en) | Plate-and -frame type membrane module system with inserted durable balls using vortex flow | |
| WO2020080953A1 (en) | A simultaneous, quadruple, low energy, high flow, gravity fed bio-filtration device with self-balancing aeration | |
| JPH02227121A (en) | Treatment by membrane | |
| US1907691A (en) | Process for purifying liquids | |
| CN211813542U (en) | Deionized water degasser | |
| JP2012166142A (en) | System for membrane separation activated sludge and method for membrane separation activated sludge | |
| Ripperger | Engineering aspects and applications of crossflow microfiltration | |
| JP3111463B2 (en) | Organic wastewater treatment equipment | |
| JPH0580247B2 (en) | ||
| JP2006255505A (en) | Biological treatment apparatus and biological treatment method | |
| JPS63221805A (en) | Filter | |
| JPH0445895A (en) | Waste water treating equipment | |
| SE518105C2 (en) | Methods and apparatus for aerating liquids |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| S111 | Request for change of ownership or part of ownership |
Free format text: JAPANESE INTERMEDIATE CODE: R313111 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |
|
| LAPS | Cancellation because of no payment of annual fees |