JPH0699018A - Membrane type polar gas separation device - Google Patents
Membrane type polar gas separation deviceInfo
- Publication number
- JPH0699018A JPH0699018A JP3017687A JP1768791A JPH0699018A JP H0699018 A JPH0699018 A JP H0699018A JP 3017687 A JP3017687 A JP 3017687A JP 1768791 A JP1768791 A JP 1768791A JP H0699018 A JPH0699018 A JP H0699018A
- Authority
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- Japan
- Prior art keywords
- gas
- polar
- polar gas
- membrane module
- carrier
- 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.)
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- Separation Using Semi-Permeable Membranes (AREA)
- Treating Waste Gases (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は膜式極性ガス分離装置に
関し、環境装置の排ガスの連続処理プロセスに有利に適
用される同装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a membrane type polar gas separation device, and more particularly to the same device which is advantageously applied to a continuous treatment process of exhaust gas of an environmental device.
【０００２】[0002]
【従来の技術】従来、排ガス中の極性ガスを分離除去す
るに際しては、一般的にゼオライト、固体アミンなどの
吸着剤を使用する吸脱着法によって行っている。このた
め、吸着操作では極性ガスの吸着剤への吸着及び極性ガ
スの吸着した吸着剤を蒸気による加熱または真空ポンプ
による減圧の２つの操作が交互に必要となる。このた
め、連続的に極性ガスを分離除去するには従来法では吸
着塔を２基設けることにより、１基を吸着、残る１基を
再生中として排ガスを連続処理している。2. Description of the Related Art Conventionally, the polar gas in exhaust gas is separated and removed by an adsorption / desorption method using an adsorbent such as zeolite or solid amine. Therefore, in the adsorption operation, two operations of adsorbing the polar gas on the adsorbent and heating the adsorbent on which the polar gas is adsorbed by steam or depressurizing by the vacuum pump are alternately required. Therefore, in order to continuously separate and remove the polar gas, in the conventional method, the exhaust gas is continuously treated by providing two adsorption towers, one for adsorbing and the other for regenerating.
【０００３】図２に従来法の一態様例を示す。この例は
吸着塔１１が吸着中、吸着塔１６が再生中を示す例であ
る。被処理ガス３は吸着塔１１に送られ、吸着塔１１内
部の吸着剤に極性ガスを吸着させ、出口より精製ガス４
を得ている。一方、吸着塔１６へは蒸気１２が送られ、
吸着塔１６内部の吸着剤を加熱することにより、吸着剤
に吸着していた極性ガス１３を脱着し、吸着剤の再生が
行われている。脱着した極性ガス１３は蒸気１２と一緒
に熱交換器１７へ送られ、ここで蒸気１２は凝縮して水
となる。凝縮してできた水と極性ガス１３は気液分離器
１８に送られ、そこで極性ガス１３と水は分離される。FIG. 2 shows an example of a conventional method. In this example, the adsorption tower 11 is adsorbing and the adsorption tower 16 is regenerating. The gas to be treated 3 is sent to the adsorption tower 11, the polar gas is adsorbed by the adsorbent inside the adsorption tower 11, and the purified gas 4 is discharged from the outlet.
Is getting On the other hand, the vapor 12 is sent to the adsorption tower 16,
By heating the adsorbent inside the adsorption tower 16, the polar gas 13 adsorbed by the adsorbent is desorbed and the adsorbent is regenerated. The desorbed polar gas 13 is sent to the heat exchanger 17 together with the steam 12, where the steam 12 condenses into water. The condensed water and the polar gas 13 are sent to the gas-liquid separator 18, where the polar gas 13 and the water are separated.
【０００４】吸着塔１１内の吸着剤が飽和し極性ガスの
吸着能力が低下するとバルブ１４とバルブ１５の開閉の
切り換えを行い、吸着塔１１は再生中、吸着塔１６は吸
着中となる。When the adsorbent in the adsorption tower 11 is saturated and the adsorption capacity for polar gas decreases, the valves 14 and 15 are switched between open and closed, the adsorption tower 11 is regenerating and the adsorption tower 16 is adsorbing.
【０００５】なお、図２中、８，１０は吸着塔１１が再
生条件になるとき、吸着塔１６の１７，１８と同じよう
に熱交換器、気液分離器として作用する機器である。In FIG. 2, 8 and 10 are devices that act as a heat exchanger and a gas-liquid separator when the adsorption tower 11 is in a regeneration condition, like the adsorption towers 17 and 18.
【０００６】[0006]
【発明が解決しようとする課題】従来法では吸着操作で
あるため、連続操作が不可能であり、吸着塔を２基設け
交互に吸着と再生を繰り返す操作になる。従って、吸着
塔が２基必要で操作が複雑になる。また、吸着剤の再生
に蒸気または減圧が必要となるのでエネルギーを大量に
必要とする。Since the conventional method is an adsorption operation, continuous operation is not possible, and two adsorption towers are provided to alternately repeat adsorption and regeneration. Therefore, two adsorption towers are required and the operation becomes complicated. In addition, a large amount of energy is required because steam or reduced pressure is required to regenerate the adsorbent.
【０００７】本発明は上記技術水準に鑑み、連続操作が
可能で、しかも操作が簡単で省エネルギーである極性ガ
ス分離装置を提供しようとするものである。In view of the above-mentioned state of the art, the present invention is to provide a polar gas separation apparatus which can be continuously operated, is easy to operate, and is energy-saving.
【０００８】[0008]
【課題を解決するための手段】本発明は循環ラインを
経て移送される極性ガス吸収液が流通する多数の疎水性
多孔質中空膜を内部に備え、かつ極性ガス含有ガス供給
口及び脱極性ガス排出口を有する極性ガス吸収用膜モジ
ュール 該極性ガス吸収用膜モジュール出口後流に設けられ、
極性ガス含有極性ガス吸収液が流通する多数の疎水性多
孔質中空膜を内部に備え、かつキャリアガス供給口及び
キャリアガスと極性ガスとの混合ガスの排出口を有する
極性ガス放散用膜モジュール 該極性ガス放散用膜モジュール出口に設けられ、前記
極性ガス吸収用膜モジュール１に極性ガス吸収液を供給
する循環ライン 前記極性ガス放散用膜モジュールの混合ガスの排出口
の後流にコンプレッサを介して設けられ、該混合ガスを
キャリアガスと極性ガスに分離する高分子分離膜を備
え、かつ極性ガス排出口及びキャリアガス排出口を有す
るガス分離膜モジュール 該ガス分離膜モジュールのキャリアガス排出口からの
キャリアガスを前記極性ガス放散用膜モジュールのキャ
リアガス供給口に供給する循環ラインを具備してなるこ
とを特徴とする膜式極性ガス分離装置である。The present invention is provided with a large number of hydrophobic porous hollow membranes in which a polar gas absorbing liquid transferred through a circulation line flows, and has a polar gas-containing gas supply port and a depolarizing gas. A polar gas absorbing membrane module having an outlet provided in the polar gas absorbing membrane module outlet wake,
A polar gas diffusion membrane module having a large number of hydrophobic porous hollow membranes through which a polar gas-containing polar gas-containing liquid flows, and having a carrier gas supply port and an outlet for a mixed gas of a carrier gas and a polar gas. Circulation line provided at the outlet of the polar gas diffusion membrane module and supplying a polar gas absorbing liquid to the polar gas absorption membrane module 1 via a compressor in the downstream of the mixed gas discharge port of the polar gas diffusion membrane module A gas separation membrane module provided with a polymer separation membrane for separating the mixed gas into a carrier gas and a polar gas, and having a polar gas outlet and a carrier gas outlet, from a carrier gas outlet of the gas separation membrane module. A circulating line for supplying a carrier gas to the carrier gas supply port of the polar gas diffusion membrane module, Is that membrane-polar gas separation apparatus.
【０００９】すなわち、本発明装置はガス中から極性ガ
ス（ＣＯ2 ，ＳＯ2 ，Ｈ2 Ｓ，ＮＨ 3 ）を分離する装置
で、以下の構成要素を有する。 疎水性多孔質膜モジュール２基、極性ガスの吸収
液、吸収液から極性ガスを放散させるキャリアガス、
極性ガスとキャリアガスを分離できる膜（高分子合成
膜）That is, the device of the present invention is designed to prevent polar gas
(CO2, SO2, H2S, NH 3) Separating device
And has the following components. Two hydrophobic porous membrane modules, absorption of polar gas
Liquid, carrier gas that diffuses polar gas from absorbing liquid,
Membrane that can separate polar gas and carrier gas (polymer synthesis
film)
【００１０】又、本発明の上記より構成される装置は下
記のように運転される。 疎水性多孔質膜１基を極性ガス吸収用の気液接触装
置として利用し、極性ガスを含んだガスより極性ガスを
吸収液に吸収分離する。 疎水性多孔質膜の残る１基を極性ガスを吸収した溶
液から極性ガスを放散させる気液接触器として使用す
る。 放散部でキャリアガスを使用して極性ガスを吸収し
た溶液から極性ガスを放散させる。 高分子合成膜を用いて極性ガスとキャリアガスを分
離する。Further, the above-mentioned apparatus of the present invention is operated as follows. One hydrophobic porous membrane is used as a gas-liquid contact device for absorbing a polar gas, and the polar gas is absorbed and separated from the gas containing the polar gas into the absorbing liquid. The remaining one group of the hydrophobic porous membrane is used as a gas-liquid contactor that diffuses polar gas from a solution that has absorbed polar gas. The carrier gas is used in the diffusion unit to diffuse the polar gas from the solution in which the polar gas is absorbed. A polar gas and a carrier gas are separated using a polymer synthetic membrane.
【００１１】[0011]
【作用】極性ガスとしてはＣＯ2 ，ＳＯ2 ，ＮＯ2 ，Ｎ
Ｏなどの酸性ガス、Ｈ2 Ｓ，ＮＨ4 などのアルカリ性ガ
スがあげられ、酸性ガスの吸収液としてはＮａ2 Ｃ
Ｏ3，Ｋ2 ＣＯ3 及びモノエタノールアミン，ジグリコ
ールアミン，ジエタノールアミン，ジイソプロパノール
アミン，トリエタノールアミン，メチルジエタノールア
ミンなどのアミン類（該アミン類には吸収促進のために
Ｈ3 ＡｓＯ3 ，Ｈ3 ＳｅＯ3 ，ＨＣｌＯを微量添加する
こともある）が、アルカリ性ガスの吸収液としてはＣＨ
3 ＣＯＯＨ，Ｈ3 ＰＯ4 ，Ｈ2 ＣＯ3 などが用いられ
る。[Function] Polar gases such as CO 2 , SO 2 , NO 2 , N
Acid gases such as O, H 2 S, alkaline gas, such as NH 4, and examples of the absorbing liquid acid gases Na 2 C
Amines such as O 3 , K 2 CO 3 and monoethanolamine, diglycolamine, diethanolamine, diisopropanolamine, triethanolamine, and methyldiethanolamine (the amines include H 3 AsO 3 , H 3 for promoting absorption). SeO 3 and HClO may be added in trace amounts), but CH is used as an alkaline gas absorption liquid.
3 COOH, etc. H 3 PO 4, H 2 CO 3 is used.
【００１２】疎水性多孔質中空膜の材質としては、一般
的に膜厚２０〜３０μｍ，多孔度４５％程度のポリプロ
ピレン，ポリエチレンが使用され、いかなる極性ガスと
吸収液の組合せにおいても使用できる。これら中空膜を
長時間使用しようとする場合には、耐久性向上のためＳ
ｉを表面にコーティングして使用してもよい。また、こ
れら中空膜の膜厚、多孔度は極性ガスと吸収液の組合せ
によらず、運転条件（処理ガス量，吸収液量など）によ
り決定される。なお、中空膜の強度、伝熱性能、物質移
動抵抗などの関係で支持層をもつ多層の中空膜も使用す
ることができる。As the material of the hydrophobic porous hollow membrane, polypropylene or polyethylene having a film thickness of 20 to 30 μm and a porosity of about 45% is generally used, and can be used in any combination of polar gas and absorbing liquid. When using these hollow membranes for a long time, S
You may coat and use i on the surface. The film thickness and porosity of these hollow membranes are determined by operating conditions (process gas amount, absorbing liquid amount, etc.), not by the combination of polar gas and absorbing liquid. A multi-layered hollow membrane having a support layer may be used because of the strength, heat transfer performance, mass transfer resistance, etc. of the hollow membrane.
【００１３】極性ガスとキャリアガスの関係は高分子分
離膜における膜透過速度の関係により、キャリアガスは
極性ガスよりも膜透過速度が速くなければならない。Ｈ
ｅが膜透過速度が一番速いのでキャリアガスとしては秀
れている。当然、キャリアガスは極性ガスと反応しない
ことが必要条件になるが、Ｈｅは全ての極性ガスと反応
しないので、この点からもキャリアガスとして一番適し
たものである。Since the relationship between the polar gas and the carrier gas is the relationship between the membrane permeation rates in the polymer separation membrane, the carrier gas must have a faster membrane permeation rate than the polar gas. H
Since e has the highest membrane permeation rate, it is an excellent carrier gas. Of course, it is a necessary condition that the carrier gas does not react with the polar gas, but since He does not react with all polar gases, He is also the most suitable as the carrier gas from this point.
【００１４】気液の接触は疎水性中空膜に無数に開いた
小さな孔（０．０１〜１μｍ）を通して行われる。すな
わち膜素材が疎水性であるため、液は膜表面にはじかれ
孔の中には入ってこない。吸収は目的ガス成分の気相と
液相の圧力差を推進力として行われる。すなわち、吸収
液には目的ガス成分は殆ど存在しないので、排ガス中の
目的ガス成分の圧力が吸収の推進力である。Gas-liquid contact is carried out through a large number of small holes (0.01 to 1 μm) opened in the hydrophobic hollow membrane. That is, since the membrane material is hydrophobic, the liquid is repelled by the membrane surface and does not enter the pores. The absorption is performed by using the pressure difference between the gas phase and the liquid phase of the target gas component as the driving force. That is, since the target gas component hardly exists in the absorbing liquid, the pressure of the target gas component in the exhaust gas is the driving force for absorption.
【００１５】放散も吸収同様、目的ガス成分の気相と液
相の圧力差を推進力として行われる。すなわち、吸収液
中には極性ガスが吸収しているので極性ガスの液濃度に
濃度に応じた圧力（蒸気圧）があり、一方、放散用ガス
中はキャリアガスが主成分で極性ガスが殆ど含まれてい
ないので極性ガスの圧力はほとんど０である。そのた
め、吸収液から放散ガス中へ極性ガスは放散する。Similarly to absorption, the diffusion is performed by using the pressure difference between the gas phase and the liquid phase of the target gas component as the driving force. That is, since the polar gas is absorbed in the absorbing liquid, there is a pressure (vapor pressure) according to the liquid concentration of the polar gas, while the carrier gas is the main component and the polar gas is almost the same in the diffusion gas. Since it is not contained, the pressure of the polar gas is almost zero. Therefore, the polar gas diffuses from the absorbing liquid into the diffused gas.
【００１６】高分子合成膜は、膜とガスとの相互作用の
違いによりガス種によって透過速度が異なる。高分子高
成膜を使用し、かつ、極性ガスと透過速度が大きく異な
るガスをキャリアガスとして使用することで、放散後の
極性ガスとキャリアガスの混合ガスからそれぞれを分離
することが可能となる。The polymer synthetic membrane has a different permeation rate depending on the gas species due to the difference in the interaction between the membrane and the gas. It is possible to separate each from the mixed gas of polar gas and carrier gas after emission by using high polymer film formation and using a gas whose permeation rate is significantly different from that of polar gas as the carrier gas. .
【００１７】[0017]
【実施例】本発明の一実施例を図１によって説明する。
この実施例は地球温暖化につながる煙道ガス中のＣＯ2
の除去を行う装置である。被処理ガス（ＣＯ2 ：数〜１
０数％，常温）３を吸収用膜モジュール１の中空膜外側
（シェル側）に流し、中空膜内部を流れている吸収液
（モノエタノール数mol ／ｌ，常温，常圧）２によりＣ
Ｏ2 を選択的に吸収させ、精製ガス（ＣＯ 2 ：１％以
下）４を得る。DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the present invention will be described with reference to FIG.
In this example, CO in flue gas leading to global warming2
It is a device for removing. Gas to be treated (CO2: Number ~ 1
Outside the hollow membrane of the absorption membrane module 1
Absorbing liquid flowing inside (hollow membrane)
(Monoethanol several mol / l, normal temperature, normal pressure) 2 C
O2Selectively absorbs the purified gas (CO 2: 1% or less
Bottom) get 4.
【００１８】ＣＯ2 ２１を吸収した吸収液２は上記と同
じ中空膜よりなる放散用膜モジュール６に給液される。
放散用膜モジュール６ではキャリアガス（１atm ，Ｈ
ｅ：主成分，ＣＯ2 ：数％）２０の働きによりＣＯ2 ２
１は吸収液２からガス中へ放散し、キャリアガス２０と
の混合ガスとなる。キャリアガス２０とＣＯ2 ２１の混
合ガス（１atm ，Ｈｅ主成分，ＣＯ2 ：数〜１０％）
は、コンプレッサ９2 の働きで１０atm に加圧され、ガ
ス分離膜（膜：ポリアセテート）モジュール７へ送られ
る。The absorption liquid 2 which has absorbed the CO 2 21 is supplied to the diffusion membrane module 6 made of the same hollow membrane as described above.
In the diffusion membrane module 6, the carrier gas (1 atm, H
e: main component, CO 2 : several%) CO 2 2 due to the action of 20
1 diffuses into the gas from the absorbing liquid 2 and becomes a mixed gas with the carrier gas 20. Mixed gas of carrier gas 20 and CO 2 21 (1 atm, He main component, CO 2 : several to 10%)
Is pressurized to 10atm by the action of the compressor 9 2, gas separation membrane (membrane: polyacetate) is sent to the module 7.
【００１９】ガス分離膜モジュール７では、キャリアガ
ス２０とＣＯ2 ２１の膜透過速度の差があるので、キャ
リアガス２０はガス分離膜をよく透過するが、ＣＯ2 ２
１はガス分離膜をほとんど透過しないので、ＣＯ2 ２１
は数１０％ＣＯ2 ，残Ｈｅとなってキャリアガス（１at
m ，Ｈｅ：主成分，ＣＯ2 ：数％）２０より分離されそ
の後回収される。一方、キャリアガス２０はリサイクル
使用に回される。In the gas separation membrane module 7, since the carrier gas 20 and the CO 2 21 have different membrane permeation rates, the carrier gas 20 permeates the gas separation membrane well, but CO 2 2
1 hardly permeates through the gas separation membrane, so CO 2 21
Is several tens of percent CO 2 and the remaining He becomes carrier gas (1 at
m, He: main component, CO 2 : several%) 20 and then recovered. On the other hand, the carrier gas 20 is recycled.
【００２０】放散用膜モジュール６を透過してＣＯ2 ２
１をほとんど放散し終えた吸収液２は、溶液ポンプ９1
により再び吸収用膜モジュール１へリサイクルされる。After passing through the diffusion membrane module 6, CO 2 2
The absorption liquid 2 which has almost completely diffused 1 is the solution pump 9 1
Is recycled to the absorption membrane module 1 again.
【００２１】吸収用膜モジュール１及び放散用膜モジュ
ール６は、概略下記仕様である。疎水性多孔質膜（素材
はポリエチレン，ポエプロピレン，ポリテトラフルオロ
エチレン等）を内径数百μｍ、肉厚数十μｍの中空糸状
にしたものを数千〜数万本を円筒容器に充填したもので
ある。The absorption membrane module 1 and the diffusion membrane module 6 have the following outline specifications. Thousands to tens of thousands of hollow porous hydrophobic membranes (materials such as polyethylene, polyethylene propylene, polytetrafluoroethylene, etc.) with an inner diameter of several hundred μm and wall thickness of several tens of μm are filled in a cylindrical container. Is.
【００２２】吸収液２はモノエタノールアミンのほかＣ
Ｏ2 の選択的吸収が行われるような薬液、例えばジエタ
ノールアミン，Ｋ2 ＣＯ3 ，ＫＨ2 ＣＯ3 ，Ｈ2 Ｏ等の
混合溶液等を使用してもよい。Absorbing liquid 2 is C in addition to monoethanolamine.
A chemical solution that selectively absorbs O 2 may be used, for example, a mixed solution of diethanolamine, K 2 CO 3 , KH 2 CO 3 , H 2 O and the like.
【００２３】ガス分離用膜モジュール７に使用される膜
は、前記のポリアセテートのほか膜とガスとの相互作用
の違いによりガス種によって透過速度が異なる高分子合
成膜ならばどのような材質の膜も使用しうる。The membrane used in the gas separation membrane module 7 is made of any material as long as it is a polymer synthetic membrane having a different permeation rate depending on the gas species due to the difference in interaction between the membrane and the gas, in addition to the above polyacetate. Membranes may also be used.
【００２４】[0024]
【発明の効果】本発明は、上記により構成されているの
で従来法に比して、（１）連続操作が可能、（２）操作
が簡単、（３）省エネルギー、（４）コンパクト（中空
膜モジュールを使用しているので、コンパクトであるが
気液接触界面を多くとれるため）である利点がある。EFFECTS OF THE INVENTION Since the present invention is constituted as described above, compared with the conventional method, (1) continuous operation is possible, (2) operation is easy, (3) energy saving, (4) compact (hollow membrane) Since the module is used, it has an advantage of being compact but being able to take many gas-liquid contact interfaces).
【図１】本発明の一実施例のフローの説明図FIG. 1 is an explanatory diagram of a flow of an embodiment of the present invention.
【図２】従来の極性ガスの分離法の一態様例のフローの
説明図FIG. 2 is an explanatory view of a flow of an example of one embodiment of a conventional polar gas separation method.
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.5 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｂ０１Ｄ 53/34 １３５ Ｚ (72)発明者 羽田 壽夫 神戸市兵庫区和田崎町一丁目１番１号 三 菱重工業株式会社神戸造船所内─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 5 Identification number Reference number within the agency FI Technical indication location B01D 53/34 135 Z (72) Inventor Toshio Haneda 1-1 1-1 Wadazaki-cho, Hyogo-ku, Kobe Sanryo Heavy Industries Co., Ltd.Kobe Shipyard
Claims (1)
吸収液が流通する多数の疎水性多孔質中空膜を内部に備
え、かつ極性ガス含有ガス供給口及び脱極性ガス排出口
を有する極性ガス吸収用膜モジュール 該極性ガス吸収用膜モジュール出口後流に設けられ、
極性ガス含有極性ガス吸収液が流通する多数の疎水性多
孔質中空膜を内部に備え、かつキャリアガス供給口及び
キャリアガスと極性ガスとの混合ガスの排出口を有する
極性ガス放散用膜モジュール 該極性ガス放散用膜モジュール出口に設けられ、前記
極性ガス吸収用膜モジュール１に極性ガス吸収液を供給
する循環ライン 前記極性ガス放散用膜モジュールの混合ガスの排出口
の後流にコンプレッサを介して設けられ、該混合ガスを
キャリアガスと極性ガスに分離する高分子分離膜を備
え、かつ極性ガス排出口及びキャリアガス排出口を有す
るガス分離膜モジュール 該ガス分離膜モジュールのキャリアガス排出口からの
キャリアガスを前記極性ガス放散用膜モジュールのキャ
リアガス供給口に供給する循環ラインを具備してなるこ
とを特徴とする膜式極性ガス分離装置。1. A polar gas absorption device having a large number of hydrophobic porous hollow membranes through which a polar gas absorption liquid transferred through a circulation line flows and having a polar gas-containing gas supply port and a depolarization gas discharge port. Membrane module provided for the polar gas absorption membrane module outlet wake,
A polar gas diffusion membrane module having a large number of hydrophobic porous hollow membranes through which a polar gas-containing polar gas-containing liquid flows, and having a carrier gas supply port and an outlet for a mixed gas of a carrier gas and a polar gas. Circulation line provided at the outlet of the polar gas diffusion membrane module and supplying a polar gas absorbing liquid to the polar gas absorption membrane module 1 via a compressor in the downstream of the mixed gas discharge port of the polar gas diffusion membrane module A gas separation membrane module provided with a polymer separation membrane for separating the mixed gas into a carrier gas and a polar gas, and having a polar gas outlet and a carrier gas outlet, from a carrier gas outlet of the gas separation membrane module. A circulating line for supplying a carrier gas to the carrier gas supply port of the polar gas diffusion membrane module, That membrane-polar gas separation apparatus.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3017687A JPH0699018A (en) | 1991-02-08 | 1991-02-08 | Membrane type polar gas separation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3017687A JPH0699018A (en) | 1991-02-08 | 1991-02-08 | Membrane type polar gas separation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0699018A true JPH0699018A (en) | 1994-04-12 |
Family
ID=11950733
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3017687A Withdrawn JPH0699018A (en) | 1991-02-08 | 1991-02-08 | Membrane type polar gas separation device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0699018A (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007283267A (en) * | 2006-04-20 | 2007-11-01 | Kansai Electric Power Co Inc:The | Gas separation process and device |
| JPWO2005119268A1 (en) * | 2004-06-02 | 2008-04-03 | アークレイ株式会社 | Analysis tool orientation selection mechanism and analyzer |
| KR101440001B1 (en) * | 2012-10-18 | 2014-09-12 | 한국화학연구원 | Biogas upgrading process and plants using microporous hollow fiber membranes |
| WO2017150721A1 (en) * | 2016-03-04 | 2017-09-08 | 旭化成株式会社 | Module for gas separation, and gas separation method |
| CN113491927A (en) * | 2020-04-01 | 2021-10-12 | 南京工业大学 | Method and device for removing carbon dioxide through multi-section membrane absorption |
| CN114502823A (en) * | 2019-10-01 | 2022-05-13 | 韩国造船海洋株式会社 | Exhaust gas treatment device |
-
1991
- 1991-02-08 JP JP3017687A patent/JPH0699018A/en not_active Withdrawn
Cited By (11)
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|---|---|---|---|---|
| JPWO2005119268A1 (en) * | 2004-06-02 | 2008-04-03 | アークレイ株式会社 | Analysis tool orientation selection mechanism and analyzer |
| JP4576549B2 (en) * | 2004-06-02 | 2010-11-10 | アークレイ株式会社 | Analysis tool orientation selection mechanism and analyzer |
| US8703054B2 (en) | 2004-06-02 | 2014-04-22 | Arkray, Inc. | Direction selection mechanism for analytical tool, and analytical device |
| JP2007283267A (en) * | 2006-04-20 | 2007-11-01 | Kansai Electric Power Co Inc:The | Gas separation process and device |
| KR101440001B1 (en) * | 2012-10-18 | 2014-09-12 | 한국화학연구원 | Biogas upgrading process and plants using microporous hollow fiber membranes |
| WO2017150721A1 (en) * | 2016-03-04 | 2017-09-08 | 旭化成株式会社 | Module for gas separation, and gas separation method |
| US11077405B2 (en) | 2016-03-04 | 2021-08-03 | Asahi Kasei Kabushiki Kaisha | Module for gas separation, and gas separation method |
| CN114502823A (en) * | 2019-10-01 | 2022-05-13 | 韩国造船海洋株式会社 | Exhaust gas treatment device |
| JP2023506680A (en) * | 2019-10-01 | 2023-02-20 | コリア シップビルディング アンド オフショア エンジニアリング カンパニー リミテッド | Exhaust gas treatment device |
| US11788449B2 (en) | 2019-10-01 | 2023-10-17 | Korea Shipbuilding & Offshore Engineering Co., Ltd. | Exhaust gas treatment apparatus |
| CN113491927A (en) * | 2020-04-01 | 2021-10-12 | 南京工业大学 | Method and device for removing carbon dioxide through multi-section membrane absorption |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A300 | Withdrawal of application because of no request for examination |
Free format text: JAPANESE INTERMEDIATE CODE: A300 Effective date: 19980514 |