JP3224409B2 - Hollow fiber membrane module for degassing - Google Patents
Hollow fiber membrane module for degassingInfo
- Publication number
- JP3224409B2 JP3224409B2 JP00172492A JP172492A JP3224409B2 JP 3224409 B2 JP3224409 B2 JP 3224409B2 JP 00172492 A JP00172492 A JP 00172492A JP 172492 A JP172492 A JP 172492A JP 3224409 B2 JP3224409 B2 JP 3224409B2
- Authority
- JP
- Japan
- Prior art keywords
- hollow fiber
- fiber membrane
- degassing
- liquid
- deaeration
- 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 - Lifetime
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- Separation Using Semi-Permeable Membranes (AREA)
- Degasification And Air Bubble Elimination (AREA)
- Physical Water Treatments (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、脱気性能を向上させた
脱気用中空糸膜モジュールに関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a hollow fiber membrane module for deaeration with improved deaeration performance.
【０００２】[0002]
【従来の技術】従来、液体中、例えば水中の溶存酸素を
脱気する方法として、例えば特開平２−２６５６０４号
公報では、物理的脱気手段とパラジウム触媒を用いる化
学的溶存酸素除去手段とを備える溶存酸素除去装置を用
いる方法が開示されている。この方法のうち物理的脱気
手段では溶存ガスの完全除去が困難で、かつ除去時間が
長い。一方、化学的溶存酸素除去手段においては、薬品
を使用するため人体への悪影響が考えられる。2. Description of the Related Art Conventionally, as a method for degassing dissolved oxygen in a liquid, for example, water, for example, Japanese Patent Application Laid-Open No. 2-265604 discloses a method in which a physical degassing means and a chemical dissolved oxygen removing means using a palladium catalyst are used. A method using a dissolved oxygen remover provided is disclosed. Of these methods, it is difficult to completely remove dissolved gas by physical degassing means, and the removal time is long. On the other hand, in the chemical dissolved oxygen removing means, the use of chemicals may have an adverse effect on the human body.
【０００３】これを解決するために、特開平３−１６９
３０３号公報では、複合中空糸膜を用いて、水溶液と接
する多孔質層と反対側の多孔質層側を減圧にして水溶液
中の溶存ガスを除去する溶存ガスの除去法が開示されて
いる。しかしながら、中空糸膜を用いて脱気を行う場
合、中空糸膜内部を流れる液体は中空糸膜の内径が小さ
いため、通常使用される圧力条件領域では層流として流
れる。その結果、中空糸膜内部を通過する液体には徐々
にその中に脱気されない部分と、溶存酸素の濃度勾配を
持つ部分（境膜）が生じ、脱気性能が低下するという問
題点があった。To solve this problem, Japanese Patent Laid-Open Publication No. 3-169
No. 303 discloses a method for removing a dissolved gas in an aqueous solution by using a composite hollow fiber membrane and reducing the pressure on the porous layer side opposite to the porous layer in contact with the aqueous solution. However, when deaeration is performed using a hollow fiber membrane, the liquid flowing inside the hollow fiber membrane flows as a laminar flow in a normally used pressure condition region because the inner diameter of the hollow fiber membrane is small. As a result, the liquid passing through the inside of the hollow fiber membrane has a problem that a portion that is not degassed gradually and a portion having a concentration gradient of dissolved oxygen (a boundary film) are formed therein, and the degassing performance is reduced. Was.
【０００４】[0004]
【発明が解決しようとする課題】本発明の目的は、かか
る従来の問題点を解決した優れた脱気性能を有する簡易
な構造の脱気用中空糸膜モジュールを提供することにあ
る。SUMMARY OF THE INVENTION An object of the present invention is to provide a hollow fiber membrane module for deaeration having a simple structure and excellent deaeration performance, which solves the conventional problems.
【０００５】[0005]
【課題を解決するための手段】すなわち、本発明は、中
空糸膜の中空部に液体を流し、中空糸膜の外周部を減圧
下に保って液体中の溶存気体を除去するための脱気用中
空糸膜モジュールにおいて、該モジュール内の各中空糸
膜の液体導入端部から液体放出端部へ至る間に各中空糸
膜を分断するように介在するとともに各中空糸膜と連通
する液体合流室が少なくとも一つ配設されてなることを
特徴とする脱気用中空糸膜モジュールである。That is, the present invention provides a deaeration for removing a dissolved gas in a liquid by flowing a liquid through the hollow portion of the hollow fiber membrane and keeping the outer peripheral portion of the hollow fiber membrane under reduced pressure. in use the hollow fiber membrane module, the hollow fiber while extending from the liquid introducing end portion of each hollow fiber membrane in the module to the liquid discharge end
A hollow fiber membrane module for degassing, comprising at least one liquid merging chamber interposed so as to divide the membrane and communicating with each hollow fiber membrane.
【０００６】[0006]
【作用】本発明の脱気用中空糸膜モジュールでは、脱気
用の中空糸膜の糸長方向の中間部に少なくとも１つの液
体合流室を形成することにより、中空糸膜内部を通過す
る液体が形成する層流を乱し、境膜を破壊して脱気効率
を向上させる。According to the hollow fiber membrane module for degassing of the present invention, at least one liquid merging chamber is formed in the middle part of the hollow fiber membrane for degassing in the yarn length direction, so that the liquid passing through the hollow fiber membrane is formed. Disturbs the laminar flow formed by, destroys the film and improves the degassing efficiency.
【０００７】[0007]
【実施例】以下、図面を参照しつつ本発明の脱気用中空
糸膜モジュールにつき説明する。図１は、本発明の脱気
用中空糸膜モジュールの一例を示す模式断面図である。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS A hollow fiber membrane module for degassing of the present invention will be described below with reference to the drawings. FIG. 1 is a schematic sectional view showing an example of the hollow fiber membrane module for deaeration of the present invention.
【０００８】本発明の脱気用中空糸膜モジュールは、基
本的には、液体入口１、液体出口２及び脱気口３を有す
るハウジング４内に、中空糸膜５がポッティング材６で
固定されて構成されてなるものであり、更にハウジング
内には少なくとも一つの液体合流室７が形成される。ハ
ウジング４内における中空糸膜の外周部に臨む空間は、
脱気室８を構成する。The hollow fiber membrane module for degassing of the present invention basically has a hollow fiber membrane 5 fixed by a potting material 6 in a housing 4 having a liquid inlet 1, a liquid outlet 2 and a degassing port 3. Further, at least one liquid merging chamber 7 is formed in the housing. The space facing the outer periphery of the hollow fiber membrane in the housing 4 is
The deaeration chamber 8 is constituted.
【０００９】液体合流室７は、液体入口１近傍の中空糸
膜の液体導入端部９と液体出口２近傍の中空糸膜の液体
放出端部１０との中間に少なくとも１個配設され、この
液体合流室７は各中空糸膜を流れて脱気された液体を合
流させて、中空糸膜内を流れるうちに形成された液体中
の境膜を破壊した後、再度液体を各中空糸膜に分配して
流して脱気を進めるために配設されたものである。した
がって、ハウジング内の全ての中空糸膜の中空部がこの
液体合流室と連通する必要はないが、できるだけ多くの
中空糸膜が液体合流室と連通していることが望ましい。
また、液体合流室の大きさは、中空糸膜内を流れる層流
を乱し、境膜が破壊できればよいので特に限定されな
い。At least one liquid merging chamber 7 is disposed between the liquid introduction end 9 of the hollow fiber membrane near the liquid inlet 1 and the liquid discharge end 10 of the hollow fiber membrane near the liquid outlet 2. The liquid merging chamber 7 joins the degassed liquids flowing through the hollow fiber membranes to break the liquid film formed while flowing through the hollow fiber membranes. It is provided to distribute and flow to and to promote deaeration. Therefore, it is not necessary that the hollow portions of all the hollow fiber membranes in the housing communicate with this liquid merging chamber, but it is desirable that as many hollow fiber membranes as possible communicate with the liquid merging chamber.
Further, the size of the liquid merging chamber is not particularly limited as long as the laminar flow flowing in the hollow fiber membrane is disturbed and the membrane is destroyed.
【００１０】また、後述する実施例にも示されるよう
に、ハウジング内に配設される中空糸膜の有効脱気機能
部（脱気室に臨んでいる部分の中空糸膜）の長さが等し
い場合には、液体合流室の数が多い程脱気効率が向上す
るので、モジュール作製上の繁雑さと、使用時の流体の
圧損の許す範囲で液体合流室の数が多いことが望まし
い。また、液体合流室は、中空糸膜の有効脱気機能部の
中間点にできるだけ近い位置に配設するほうが脱気効率
は向上する。なお、液体合流室の配設個数に応じて脱気
室の数は増すが、この場合、各脱気室をモジュール内で
連通させれば、脱気口の数は一つですみ、脱気室を減圧
にする操作も容易に実施できるので好ましい。Further, as shown in an embodiment described later, the length of the effective degassing function of the hollow fiber membrane (the hollow fiber membrane facing the degassing chamber) of the hollow fiber membrane provided in the housing is reduced. If they are equal to each other, the deaeration efficiency increases as the number of liquid merging chambers increases. Therefore, it is desirable that the number of liquid merging chambers be large as far as the complexity of module production and the pressure loss of the fluid during use allow. Further, the deaeration efficiency is improved by disposing the liquid merging chamber at a position as close as possible to an intermediate point of the effective deaeration function section of the hollow fiber membrane. The number of degassing chambers increases according to the number of liquid merging chambers, but in this case, if each degassing chamber is connected within the module, only one degassing port is required, The operation of reducing the pressure of the chamber can be easily performed, which is preferable.
【００１１】本発明の脱気用中空糸膜モジュールに用い
る中空糸膜としては、水が漏れ出さない程度の細孔径を
有する多孔質層のみからなるもの、細孔のない均質層の
みからなるものおよび多孔質層と均質層の組合せによる
ものなどを用いることができるが、ガス透過機能を持つ
均質層と補強機能を持つ多孔質層から構成される複合中
空糸膜を用いるのが好ましい。The hollow fiber membrane used in the hollow fiber membrane module for degassing of the present invention comprises a porous layer having a pore size such that water does not leak out, or a homogeneous layer having no pores. Although a combination of a porous layer and a homogeneous layer can be used, it is preferable to use a composite hollow fiber membrane composed of a homogeneous layer having a gas permeable function and a porous layer having a reinforcing function.
【００１２】かかる複合中空糸膜の均質層を構成するポ
リマー素材としては、ガス透過性の優れたシリコンゴム
系ポリマーを始めとして、ポリジメチルシロキサン、シ
リコンとポリカーボネートの共重合体等のシリコンゴム
系ポリマー、ポリ−４−メチルペンテン−１、線状低密
度ポリエチレン等のポリオレフィン系ポリマー、パーフ
ルオロアルキル系ポリマー等のフッ素含有ポリマー、エ
チルセルロース等のセルロース系ポリマー、ポリフェニ
レンオキサイド、ポリ−４−ビニルピリジン、ウレタン
系ポリマーおよびこれらポリマー素材の共重合体あるい
はブレンド体等の各種ポリマーを挙げることができる。Examples of the polymer material constituting the homogeneous layer of the composite hollow fiber membrane include silicone rubber-based polymers such as silicone rubber-based polymers having excellent gas permeability, polydimethylsiloxane, and copolymers of silicon and polycarbonate. Polyolefin polymers such as poly-4-methylpentene-1, linear low-density polyethylene, fluorine-containing polymers such as perfluoroalkyl polymers, cellulosic polymers such as ethylcellulose, polyphenylene oxide, poly-4-vinylpyridine, and urethane Examples include various polymers such as a base polymer and a copolymer or blend of these polymer materials.
【００１３】また、多孔質層を構成するポリマー素材と
しては、ポリエチレン、ポリプロピレン、ポリ−３−メ
チルブデン−１、ポリ−４−メチルペンテン−１等のポ
リオレフィン系ポリマー、ポリフッ化ビニリデン、ポリ
テトラフルオロエチレン等のフッ素系ポリマー、ポリス
チレン、ポリエーテルエーテルケトン等の疎水性ポリマ
ーが挙げられる。The polymer material constituting the porous layer includes polyolefin polymers such as polyethylene, polypropylene, poly-3-methylbutene-1, and poly-4-methylpentene-1, polyvinylidene fluoride, and polytetrafluoroethylene. And hydrophobic polymers such as polystyrene and polyetheretherketone.
【００１４】均質層を構成するポリマー素材と、多孔質
層を構成するポリマー素材との組合せについては特に限
定されず、異種のポリマーはもちろん同種のポリマーで
あってもよい。均質層が多孔質層で物理的に挟まれたサ
ンドイッチ構造を有するものの場合には、両膜間の接着
性が悪くとも、実用上の弊害は生じない。The combination of the polymer material constituting the homogeneous layer and the polymer material constituting the porous layer is not particularly limited, and different types of polymers may be used, of course. In the case where the homogeneous layer has a sandwich structure physically sandwiched between porous layers, even if the adhesion between the two layers is poor, no practical adverse effect occurs.
【００１５】多孔質層は、均質層を補強し保護する機能
を主としているので、複合中空糸膜全体としてのガス透
過能に大きな制約を加えない程度の細孔を有するもので
あれば、その細孔の大きさ等については特に制限されな
い。The porous layer mainly has the function of reinforcing and protecting the homogeneous layer. Therefore, if the porous layer has pores that do not greatly restrict the gas permeability of the composite hollow fiber membrane as a whole, its fineness is small. The size of the holes and the like are not particularly limited.
【００１６】このような複合中空糸膜は、例えば多重円
筒型の紡糸ノズルを用いて、均質層を形成するポリマー
と、多孔質層を形成するポリマーとを交互にかつ均質層
を形成するポリマーがサンドイッチされるよう配置して
溶融紡糸し、次いで均質層の部分を多孔質化することな
く、多孔質層の部分だけが多孔質化される条件で延伸す
る方法によって製造することができる。[0016] Such a composite hollow fiber membrane is formed by alternately and uniformly forming a polymer forming a homogeneous layer and a polymer forming a porous layer using a multi-cylindrical spinning nozzle. It can be produced by a method in which it is arranged so as to be sandwiched, melt-spun, and then stretched under the condition that only the portion of the porous layer is made porous without making the portion of the homogeneous layer porous.
【００１７】以下、実施例により、本発明をより具体的
に説明する。Hereinafter, the present invention will be described more specifically with reference to examples.
【００１８】実施例１ 多孔質中空糸膜（ポリエチレン多層複合中空糸膜、ＭＨ
Ｆ２００Ｍ、三菱レイヨン（株）製）を用い、液体合流
室を１つ有する図１のような構造の脱気用中空糸膜モジ
ュールを作製した。この脱気用中空糸膜モジュール中
を、下記の条件で水を通過させ、水中の溶存酸素濃度
（単位：ｐｐｍ）を測定し、脱気性能を評価した。結果
を図５に示した。 水（脱気前）の平均溶存酸素濃度 ７．６２ppm 平均水温 ２８．２３℃ 減圧側平均真空度 ５９．１Torr 真空ポンプ出ガスの平均酸素濃度 ３１．３０vol ％ 中空糸膜内径 ２００μm 中空糸膜厚 ２５μm 中空糸膜有効長 ２６０mm（ｌ1 ＝１３０mm、ｌ2 ＝１３０mm） 中空糸膜本数 １１，５２０本 通水量 １リットル／min. 実施例２ 図２に示すような液体合流室を２つ有する脱気用中空糸
膜モジュールを用いた以外は、実施例１と同様の条件に
よりモジュールの脱気性能を測定した。なお、中空糸膜
有効長はｌ3 ＝ｌ4 ＝ｌ5 ＝２６０／３ｍｍである。評
価結果を図５に示した。Example 1 Porous hollow fiber membrane (polyethylene multilayer composite hollow fiber membrane, MH
Using F200M, manufactured by Mitsubishi Rayon Co., Ltd., a hollow fiber membrane module for deaeration having a structure as shown in FIG. 1 having one liquid merging chamber was produced. Water was passed through this hollow fiber membrane module for degassing under the following conditions, and the dissolved oxygen concentration (unit: ppm) in the water was measured to evaluate the degassing performance. The results are shown in FIG. Average dissolved oxygen concentration of water (before degassing) 7.62 ppm Average water temperature 28.23 ° C. Average degree of vacuum on decompression side 59.1 Torr Average oxygen concentration of gas discharged from vacuum pump 31.30 vol% Inner diameter of hollow fiber membrane 200 μm Thickness of hollow fiber 25 μm Effective length of hollow fiber membrane 260 mm (l 1 = 130 mm, l 2 = 130 mm) Number of hollow fiber membranes 11,520 Water flow 1 liter / min. Example 2 Deaeration having two liquid merging chambers as shown in FIG. The degassing performance of the module was measured under the same conditions as in Example 1 except that the hollow fiber membrane module for use was used. The effective length of the hollow fiber membrane is l 3 = l 4 = l 5 = 260/3 mm. The evaluation results are shown in FIG.
【００１９】実施例３ 図３に示すような液体合流室を３つ有する脱気用中空糸
膜モジュールを用いた以外は、実施例１と同様の条件に
よりモジュールの脱気性能を測定した。なお、中空糸膜
有効長はｌ6 ＝ｌ7 ＝ｌ8 ＝ｌ9 ＝２６０／４ｍｍであ
る。評価結果を図５に示した。Example 3 The degassing performance of the module was measured under the same conditions as in Example 1 except that a hollow fiber membrane module for deaeration having three liquid merging chambers as shown in FIG. 3 was used. The effective length of the hollow fiber membrane is l 6 = l 7 = l 8 = l 9 = 260/4 mm. The evaluation results are shown in FIG.
【００２０】実施例４ ｌ1 ＝１０ｍｍ、ｌ2 ＝２５０ｍｍであることを除いて
は実施例１と全く同様な図１に示すような脱気用中空糸
膜モジュールを用いた以外は、実施例１と同様の条件に
よりモジュールの脱気性能を測定した。評価結果を図５
に示した。Example 4 Example 1 was the same as Example 1 except that l 1 = 10 mm and l 2 = 250 mm, except that a hollow fiber membrane module for deaeration as shown in FIG. 1 was used. The degassing performance of the module was measured under the same conditions as in 1. Figure 5 shows the evaluation results.
It was shown to.
【００２１】実施例５ ｌ1 ＝２５０ｍｍ、ｌ2 ＝１０ｍｍであることを除いて
は実施例１と全く同様な図１に示すような脱気用中空糸
膜モジュールを用いた以外は、実施例１と同様の条件に
よりモジュールの脱気性能を測定した。評価結果を図５
に示した。Example 5 Example 1 was the same as Example 1 except that l 1 = 250 mm and l 2 = 10 mm, except that a hollow fiber membrane module for deaeration as shown in FIG. 1 was used. The degassing performance of the module was measured under the same conditions as in 1. Figure 5 shows the evaluation results.
It was shown to.
【００２２】実施例６ ｌ1 ＝２００ｍｍ、ｌ2 ＝６０ｍｍであることを除いて
は実施例１と全く同様な図１に示すような脱気用中空糸
膜モジュールを用いた以外は、実施例１と同様の条件に
よりモジュールの脱気性能を測定した。評価結果を図５
に示した。Example 6 Example 1 was the same as Example 1 except that l 1 = 200 mm and l 2 = 60 mm, except that a hollow fiber membrane module for deaeration as shown in FIG. 1 was used. The degassing performance of the module was measured under the same conditions as in 1. Figure 5 shows the evaluation results.
It was shown to.
【００２３】実施例７ ｌ1 ＝６０ｍｍ、ｌ2 ＝２００ｍｍであることを除いて
は実施例１と全く同様な図１に示すような脱気用中空糸
膜モジュールを用いた以外は、実施例１と同様の条件に
よりモジュールの脱気性能を測定した。評価結果を図５
に示した。Example 7 Example 1 was the same as Example 1 except that l 1 = 60 mm and l 2 = 200 mm, except that a hollow fiber membrane module for deaeration as shown in FIG. 1 was used. The degassing performance of the module was measured under the same conditions as in 1. Figure 5 shows the evaluation results.
It was shown to.
【００２４】比較例１ 図４に示すような液体合流室のない従来のタイプの脱気
用中空糸膜モジュールを用いた以外は、実施例１と同様
の条件によりモジュールの脱気性能を測定した。なお、
中空糸膜有効長はｌ0 ＝２６０である。評価結果を図５
に示した。Comparative Example 1 The deaeration performance of the module was measured under the same conditions as in Example 1 except that a conventional type of deaeration hollow fiber membrane module having no liquid merging chamber as shown in FIG. 4 was used. . In addition,
The effective length of the hollow fiber membrane is l 0 = 260. Figure 5 shows the evaluation results.
It was shown to.
【００２５】[0025]
【発明の効果】本発明により、脱気性能が大幅に向上し
た脱気用中空糸膜モジュールが提供され、ボイラー配管
の防錆、ビル・マンションの水道給水配管の赤水防止、
高集積度半導体製造用超純水の溶存酸素除去及び食品関
係の用途に有効に用いることができる。According to the present invention, there is provided a hollow fiber membrane module for deaeration with greatly improved deaeration performance, rust prevention of boiler pipes, prevention of red water of water supply pipes of buildings and condominiums,
It can be effectively used for removing dissolved oxygen from ultrapure water for manufacturing highly integrated semiconductors and for food-related applications.
【図１】本発明の脱気用中空糸膜モジュールの一例を示
す模式断面図である。FIG. 1 is a schematic sectional view showing an example of a hollow fiber membrane module for degassing of the present invention.
【図２】本発明の脱気用中空糸膜モジュールの他の一例
を示す模式断面図である。FIG. 2 is a schematic sectional view showing another example of the hollow fiber membrane module for deaeration of the present invention.
【図３】本発明の脱気用中空糸膜モジュールの他の一例
を示す模式断面図である。FIG. 3 is a schematic sectional view showing another example of the hollow fiber membrane module for deaeration of the present invention.
【図４】従来の脱気用中空糸膜モジュールの一例を示す
模式断面図である。FIG. 4 is a schematic sectional view showing an example of a conventional hollow fiber membrane module for deaeration.
【図５】各種の脱気用中空糸膜モジュールを使用して脱
気性能を測定した際のモジュール通水量と、モジュール
通過水のモジュール出口における酸素濃度の関係を示し
たグラフである。FIG. 5 is a graph showing the relationship between the amount of water passing through the module and the oxygen concentration at the module outlet when the degassing performance is measured using various types of hollow fiber membrane modules for degassing.
１ 液体入口 ２ 液体出口 ３ 脱気口 ４ ハウジング ５ 中空糸膜 ６ ポッティング材 ７ 液体合流室 ８ 脱気室 ９ 液体導入端部 １０ 液体放出端部 DESCRIPTION OF SYMBOLS 1 Liquid inlet 2 Liquid outlet 3 Deaeration port 4 Housing 5 Hollow fiber membrane 6 Potting material 7 Liquid merging chamber 8 Deaeration chamber 9 Liquid introduction end 10 Liquid discharge end
───────────────────────────────────────────────────── フロントページの続き (72)発明者 菊屋 信之 広島県大竹市御幸町20番１号 三菱レイ ヨン株式会社中央研究所内 (72)発明者 平井 孝之 広島県大竹市御幸町20番１号 三菱レイ ヨン株式会社中央研究所内 (56)参考文献 特開 平４−247224（ＪＰ，Ａ) 特開 平１−180204（ＪＰ，Ａ) 特開 平１−239621（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) B01D 19/00 B01D 63/02 - 63/04 C02F 1/20 B01D 53/22 ──────────────────────────────────────────────────続 き Continued on the front page (72) Inventor Nobuyuki Kikuya 20-1 Miyukicho, Otake City, Hiroshima Prefecture Inside Mitsubishi Rayon Co., Ltd. (72) Inventor Takayuki Hirai 20-1 Miyukicho, Otake City, Hiroshima Prefecture Mitsubishi (56) References JP-A-4-247224 (JP, A) JP-A-1-180204 (JP, A) JP-A-1-239621 (JP, A) (58) Field (Int.Cl. 7 , DB name) B01D 19/00 B01D 63/02-63/04 C02F 1/20 B01D 53/22
Claims (1)
膜の外周部を減圧下に保って液体中の溶存気体を除去す
るための脱気用中空糸膜モジュールにおいて、該モジュ
ール内の各中空糸膜の液体導入端部から液体放出端部へ
至る間に各中空糸膜を分断するように介在するとともに
各中空糸膜と連通する液体合流室が少なくとも一つ配設
されてなることを特徴とする脱気用中空糸膜モジュー
ル。1. A degassing hollow fiber membrane module for flowing a liquid through a hollow portion of a hollow fiber membrane and removing a dissolved gas in the liquid while maintaining an outer peripheral portion of the hollow fiber membrane under reduced pressure. liquid merging chamber communicating with the hollow fiber membrane together when interposed so as to divide the respective hollow fiber membranes while the liquid introducing end portion extending into the liquid discharge end of the hollow fiber membrane is at least one arrangement of A hollow fiber membrane module for degassing, comprising:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP00172492A JP3224409B2 (en) | 1992-01-08 | 1992-01-08 | Hollow fiber membrane module for degassing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP00172492A JP3224409B2 (en) | 1992-01-08 | 1992-01-08 | Hollow fiber membrane module for degassing |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH05184812A JPH05184812A (en) | 1993-07-27 |
| JP3224409B2 true JP3224409B2 (en) | 2001-10-29 |
Family
ID=11509515
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP00172492A Expired - Lifetime JP3224409B2 (en) | 1992-01-08 | 1992-01-08 | Hollow fiber membrane module for degassing |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3224409B2 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE69837974T2 (en) * | 1997-04-30 | 2008-02-21 | Mitsubishi Rayon Co., Ltd. | DEVICE AND METHOD FOR DEHUMIDIFYING INK AND METHOD FOR PRODUCING INK CARTRIDGES |
| US6248157B1 (en) * | 1999-08-20 | 2001-06-19 | Systec Inc. | Vacuum degassing |
| JP5080781B2 (en) * | 2006-11-06 | 2012-11-21 | 三菱レイヨン株式会社 | Hollow fiber membrane module for degassing and degassing device |
| US8631788B2 (en) * | 2007-06-02 | 2014-01-21 | Arnold J. Landé | Artificial gills for deep diving without incurring the bends and for scavenging O2 from and dispelling CO2 into water or thin air |
| JP5378180B2 (en) | 2009-12-02 | 2013-12-25 | 愛三工業株式会社 | Separation membrane module and evaporative fuel processing apparatus having the same |
-
1992
- 1992-01-08 JP JP00172492A patent/JP3224409B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH05184812A (en) | 1993-07-27 |
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