JPH0312307A - Method for enriching oxygen - Google Patents
Method for enriching oxygenInfo
- Publication number
- JPH0312307A JPH0312307A JP1145686A JP14568689A JPH0312307A JP H0312307 A JPH0312307 A JP H0312307A JP 1145686 A JP1145686 A JP 1145686A JP 14568689 A JP14568689 A JP 14568689A JP H0312307 A JPH0312307 A JP H0312307A
- Authority
- JP
- Japan
- Prior art keywords
- oxygen
- gas
- membrane
- separation device
- air
- 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
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 239000001301 oxygen Substances 0.000 title claims abstract description 53
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 17
- 239000007789 gas Substances 0.000 claims abstract description 69
- 238000001179 sorption measurement Methods 0.000 claims abstract description 50
- 239000012528 membrane Substances 0.000 claims abstract description 41
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 40
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 20
- 239000002994 raw material Substances 0.000 claims abstract description 14
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 12
- 239000003463 adsorbent Substances 0.000 claims abstract description 12
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000010457 zeolite Substances 0.000 claims abstract description 12
- 230000001172 regenerating effect Effects 0.000 claims abstract description 5
- 238000000926 separation method Methods 0.000 claims description 45
- 230000008929 regeneration Effects 0.000 claims description 6
- 238000011069 regeneration method Methods 0.000 claims description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 28
- 238000004140 cleaning Methods 0.000 abstract description 17
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 14
- 239000001569 carbon dioxide Substances 0.000 abstract description 13
- 239000002699 waste material Substances 0.000 abstract 2
- 239000002912 waste gas Substances 0.000 abstract 1
- 238000011084 recovery Methods 0.000 description 7
- 238000003795 desorption Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 239000012141 concentrate Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 230000000274 adsorptive effect Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 229920005597 polymer membrane Polymers 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000001856 Ethyl cellulose Substances 0.000 description 1
- ZZSNKZQZMQGXPY-UHFFFAOYSA-N Ethyl cellulose Chemical compound CCOCC1OC(OC)C(OCC)C(OCC)C1OC1C(O)C(O)C(OC)C(CO)O1 ZZSNKZQZMQGXPY-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229920002301 cellulose acetate Polymers 0.000 description 1
- 238000009795 derivation Methods 0.000 description 1
- 239000002274 desiccant Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229920001249 ethyl cellulose Polymers 0.000 description 1
- 235000019325 ethyl cellulose Nutrition 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000000377 silicon dioxide 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Gases By Adsorption (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、酸素の濃縮方法に関し、詳しくは、膜分離装
置を用いて酸素濃度４０％以上の酸素富化ガスを製造す
る方法に関する。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a method for concentrating oxygen, and more particularly to a method for producing oxygen-enriched gas with an oxygen concentration of 40% or more using a membrane separation device.
従来から、空気を膜分離装置に導入して酸素を濃縮する
ことが行われているが、通常の１段の膜分離では、４０
％以上の酸素濃度を得ることが困難なため、膜分離装置
を２段以上直列に配置して酸素を濃縮する必要があった
。Conventionally, air is introduced into a membrane separation device to concentrate oxygen, but in normal one-stage membrane separation, 40
Since it is difficult to obtain an oxygen concentration of more than %, it has been necessary to arrange two or more membrane separators in series to concentrate oxygen.
また、天然または合成ゼオライトを吸着剤として用いて
空気から窒素を得る圧力変動吸着分離装置から排出され
る排ガスは、該排ガス中に酸素が濃縮されているにも拘
らず、従来、そのまま放出排ガスとされていた。In addition, the exhaust gas discharged from a pressure fluctuation adsorption separation device that uses natural or synthetic zeolite as an adsorbent to obtain nitrogen from air has conventionally been treated as discharged exhaust gas as it is, even though oxygen is concentrated in the exhaust gas. It had been.
しかしながら、上記天然または合成ゼオライトを吸着剤
として用いて窒素を得る圧力変動吸着分離装置から排出
される排ガスは、酸素が濃縮されている上、炭酸ガスや
水分をほとんど含んでいない。従って、この排ガスを原
料として膜分離を行うと膜分離装置による酸素濃縮工程
が極めてスム−スに行なわれるばかりでなく、膜分離装
置から得られる酸素富化ガス中に炭酸ガスや水分を、殆
ど含んでいないため酸素富化ガスの使用目的によっては
非常に好ましい。However, the exhaust gas discharged from a pressure fluctuation adsorptive separation device for obtaining nitrogen using the natural or synthetic zeolite as an adsorbent is enriched in oxygen and contains almost no carbon dioxide or water. Therefore, if membrane separation is performed using this exhaust gas as a raw material, not only will the oxygen concentration process by the membrane separator be performed extremely smoothly, but also carbon dioxide and moisture will be almost completely removed from the oxygen-enriched gas obtained from the membrane separator. Since it does not contain oxygen, it is very preferable depending on the intended use of the oxygen-enriched gas.
そこで、本発明は、炭酸ガスや水分の含有量が少なく、
酸素濃度が４０％以上の酸素富化ガスを容易に得ること
のできる酸素の濃縮方法を提供することを目的としてい
る。Therefore, the present invention has a low content of carbon dioxide gas and water, and
It is an object of the present invention to provide a method for concentrating oxygen that can easily obtain an oxygen-enriched gas having an oxygen concentration of 40% or more.
上記した目的を達成するために、本発明の酸素の濃縮方
法は、空気を原料として該空気中の酸素を濃縮する方法
において、天然又は合成ゼオライトを吸着剤に使用して
原料空気から窒素を回収する圧力変動吸着分離装置の後
段に酸素富化膜を設けた膜分離装置を配設し、前記圧力
変動吸着分離装置から排出される洗浄排ガスを所定圧力
に昇圧して前記膜分離装置に供給することを特徴として
いる。In order to achieve the above object, the oxygen concentration method of the present invention uses natural or synthetic zeolite as an adsorbent to recover nitrogen from the raw air in a method of concentrating oxygen in the air using air as a raw material. A membrane separator equipped with an oxygen enrichment membrane is disposed downstream of the pressure fluctuation adsorption separation device, and the washed exhaust gas discharged from the pressure fluctuation adsorption separation device is pressurized to a predetermined pressure and supplied to the membrane separation device. It is characterized by
さらに本発明は、前記膜分離装置から排出される排ガス
を、前記圧力変動吸着分離装置に供給する原料空気の前
処理を行う前処理装置の吸着塔を再生する再生ガスに用
いることも含むものである。Furthermore, the present invention includes using the exhaust gas discharged from the membrane separation device as a regeneration gas for regenerating an adsorption tower of a pretreatment device that pretreats the feed air to be supplied to the pressure fluctuation adsorption separation device.
上記のごとく、天然又は合成ゼオライトを吸着剤に使用
した窒素採取用の圧力変動吸着分離装置から排出される
洗浄排ガスは、酸素濃度が空気の２倍以上に濃縮されて
いるとともに、炭酸ガス。As mentioned above, the cleaning exhaust gas discharged from a pressure fluctuation adsorption separation device for nitrogen collection that uses natural or synthetic zeolite as an adsorbent has an oxygen concentration more than twice that of air, and contains carbon dioxide gas.
水分の含有量が極めて少ない。従って、この洗浄排ガス
を膜分離装置の原料ガスとすることで、炭酸ガス、水分
の含有量が極めて少なく、酸素濃度が４０％以上の酸素
富化ガスを容易に得ることができる。Water content is extremely low. Therefore, by using this washed exhaust gas as the raw material gas for the membrane separation device, it is possible to easily obtain an oxygen-enriched gas with extremely low carbon dioxide and water contents and an oxygen concentration of 40% or more.
以下、本発明を図面に示す一実施例に基づいて、さらに
詳細に説明する。Hereinafter, the present invention will be explained in more detail based on an embodiment shown in the drawings.
まず、天然又は合成ゼオライトを吸着剤に使用して原料
空気から窒素を回収する圧力変動吸着分離装置１０は、
例えば、前記天然又は合成ゼオライトを充填した３基の
吸着塔１１ ａ ＋ １１− ｂ 、 １１ｃを並
列に接続し、各吸着塔１．１ａ、１１ｂ。First, the pressure fluctuation adsorptive separation device 10 uses natural or synthetic zeolite as an adsorbent to recover nitrogen from feed air.
For example, three adsorption towers 11a + 11-b, 11c filled with the natural or synthetic zeolite are connected in parallel, and each adsorption tower 1.1a, 11b.
１１ｃについて吸着、洗浄、脱着の各工程を順次切替え
て空気中の窒素を分離するものである。ここで、第１塔
１１ａが吸着工程、第２塔１１ｂが洗浄工程、第３塔１
１ｃが脱着工程にある場合について説明する。11c, nitrogen in the air is separated by sequentially switching the steps of adsorption, cleaning, and desorption. Here, the first column 11a is an adsorption process, the second column 11b is a washing process, and the third column 1
A case where 1c is in the desorption process will be explained.
まず吸着工程にある第１塔１１Ｈには、水分や炭酸ガス
を除去する吸着剤を充填した吸着塔（図示せず）を有す
る前処理装置１２から原料空気弁１３を介して供給され
る所定圧力の原料空気ＧＡが、該第１塔１１ａに附随す
る吸着塔人口側の導入弁１４ａから導入される。この原
料空気ＧＡ中の窒素は、塔内の吸着剤に吸着され、他の
酸素等の弱吸着成分が出口側に濃縮する。First, the first column 11H in the adsorption step is supplied with a predetermined pressure via the raw air valve 13 from the pretreatment device 12 having an adsorption column (not shown) filled with an adsorbent for removing moisture and carbon dioxide. The feed air GA is introduced from the introduction valve 14a on the adsorption tower intake side attached to the first tower 11a. Nitrogen in this raw air GA is adsorbed by an adsorbent in the column, and other weakly adsorbed components such as oxygen are concentrated on the outlet side.
この時、洗浄工程にある第２塔１１ｂにおいては、吸着
塔入口側の洗浄弁１５ｂを開いて回収タンク１６に回収
されている高濃度窒素を洗浄ガスＦＧとしてブロワ−１
７により所定の圧力で原料空気と同方向に導入するとと
もに、吸着塔出口側の導出弁１８ｂから排気弁１９を介
して前記弱吸着成分を洗浄排ガスＷＧとして導出する。At this time, in the second tower 11b in the cleaning process, the cleaning valve 15b on the adsorption tower inlet side is opened and the high concentration nitrogen recovered in the recovery tank 16 is used as cleaning gas FG to be sent to the blower 1.
7, the weakly adsorbed components are introduced in the same direction as the raw material air at a predetermined pressure, and the weakly adsorbed components are led out as cleaning exhaust gas WG from the outlet valve 18b on the adsorption tower outlet side via the exhaust valve 19.
この洗浄排ガスＷＧは、前記吸着工程で吸着塔１１ｂの
出口側に濃縮された酸素を含むものであり、通常は空気
の２倍程度にまで酸素が濃縮されている。This cleaning exhaust gas WG contains oxygen concentrated on the outlet side of the adsorption tower 11b in the adsorption step, and usually the oxygen is concentrated to about twice that of air.
そして脱着工程にある第３塔１１−Ｃは、吸着塔出口側
の回収弁２０ｃを開き、真空ポンプ２］により吸着塔１
１ｃ内を排気して吸着剤に吸着されている窒素を回収ガ
スＧＮとして回収タンク１６に回収する。このようにし
て回収タンク１６に回収された窒素は、その一部が製品
高濃度窒素ＰＮとして弁２２から導出され、残部が前記
洗浄工程に用いる洗浄ガスＦＧとして使用される。The third column 11-C, which is in the desorption process, opens the recovery valve 20c on the outlet side of the adsorption column, and the vacuum pump 2]
The inside of 1c is evacuated and the nitrogen adsorbed by the adsorbent is recovered into the recovery tank 16 as recovery gas GN. Part of the nitrogen recovered in the recovery tank 16 in this way is led out from the valve 22 as product high concentration nitrogen PN, and the remainder is used as the cleaning gas FG used in the cleaning process.
以下、順次それぞれの弁を所定の順序で開閉することに
より、各吸着塔１１ａ、ｌｌｂ、ｌｌｃを上記吸着、洗
浄、脱着の各工程に切替えて製品高濃度窒素ＰＮを採取
する。上記工程中、上記説明で挙げた以外の６弁は閉じ
状態である。尚、上記説明で挙げた以外の６弁について
は、対応する吸着塔に付した符号ａ、ｂ、ｃをそれぞれ
の弁の符号に付して図示し、その詳細な説明を省略する
。Thereafter, by sequentially opening and closing the respective valves in a predetermined order, each adsorption tower 11a, llb, llc is switched to each of the adsorption, washing, and desorption steps, and the product high concentration nitrogen PN is collected. During the above process, six valves other than those mentioned in the above explanation are in a closed state. It should be noted that the six valves other than those mentioned in the above description are illustrated with the symbols a, b, and c attached to the corresponding adsorption towers attached to the respective valve symbols, and detailed explanation thereof will be omitted.
一方、上記圧力変動吸着分離装置１０の後段に配設され
る膜分離装置３０は、酸素を濃縮するための分離膜３１
として、高分子膜５ シリカベース膜、酢酸セルロース
膜、エチルセルロース膜２分子篩炭素膜等を備えたもの
で、−火室３２の一側には原料ガス導入部３３が設けら
れるとともに、他側には排ガス導出部３４が設けられ、
分離膜３１を介した二次室３５には酸素富化ガスＧＯの
導出部３６が設けられている。On the other hand, a membrane separation device 30 disposed downstream of the pressure fluctuation adsorption separation device 10 has a separation membrane 31 for concentrating oxygen.
The polymer membrane 5 is equipped with a silica-based membrane, a cellulose acetate membrane, an ethyl cellulose membrane, a bimolecular sieve carbon membrane, etc. - A raw material gas introduction part 33 is provided on one side of the firebox 32, and a raw material gas introduction part 33 is provided on the other side of the firebox 32. An exhaust gas derivation section 34 is provided,
The secondary chamber 35 via the separation membrane 31 is provided with an outlet section 36 for the oxygen-enriched gas GO.
そして、上記圧力変動吸着分離装置１０から排出される
洗浄排ガスＷＧは、前記弁１つを出た後で圧縮機３７に
より、膜分離に必要な圧力、通常は数ｌａｇ ／ ｃｌ
Ｇまで昇圧され、前記原料ガス導入部３３から一火室
３２に導入される。分離膜３１を透過して二次室３５に
濃縮された酸素富化ガスＧＯは、前記導出部３６から製
品として導出され、排ガスＭＧは一火室３２の排ガス導
出部３４から導出される。The washed exhaust gas WG discharged from the pressure fluctuation adsorption separation device 10 is compressed by the compressor 37 after exiting the one valve to a pressure required for membrane separation, usually several lag/cl.
The pressure is increased to G, and the raw material gas is introduced into the first fire chamber 32 from the raw material gas introduction section 33. The oxygen-enriched gas GO that has passed through the separation membrane 31 and is concentrated in the secondary chamber 35 is led out as a product from the outlet section 36, and the exhaust gas MG is led out from the exhaust gas outlet section 34 of the first fire chamber 32.
このように、前記圧力変動吸着分離装置１０から排出さ
れた洗浄排ガスＷＧを膜分離装置３０の原料ガスとする
ので、該膜分離装置３０から得られる酸素富化ガスＧＯ
の酸素濃度を高めることができ、酸素濃度４０％以上の
濃縮酸素を得ることができる。しかも原料ガスとなる洗
浄排ガスＷＧは、圧力変動吸着分離装置１０の前処理装
置１２で水分や炭酸ガスが除去されているので、これら
の不純物成分を含まない良質の酸素富化ガスＧ。In this way, since the washed exhaust gas WG discharged from the pressure fluctuation adsorption separation device 10 is used as the raw material gas for the membrane separation device 30, the oxygen-enriched gas GO obtained from the membrane separation device 30
The oxygen concentration can be increased, and concentrated oxygen with an oxygen concentration of 40% or more can be obtained. Moreover, since the cleaning exhaust gas WG, which becomes the raw material gas, has moisture and carbon dioxide removed in the pretreatment device 12 of the pressure fluctuation adsorption separation device 10, it is a high-quality oxygen-enriched gas G that does not contain these impurity components.
を得ることができる。can be obtained.
また、上記排ガスＭＧは、上記のごとく水分や炭酸ガス
をほとんど含まないため、管３８により前記前処理装置
１２の吸着塔を再生するための再生ガスとして使用する
ことができる。さらに、前記圧縮機３７の前段に、洗浄
排ガスＷＧを貯留するバッファタンクを設けることによ
り、膜分離装置３０に導入するガスの組成を安定化する
とともに、圧縮機３７の吸入圧力を安定化させることが
できる。Furthermore, since the exhaust gas MG contains almost no moisture or carbon dioxide as described above, it can be used as a regeneration gas for regenerating the adsorption tower of the pretreatment device 12 through the pipe 38. Furthermore, by providing a buffer tank for storing the washed exhaust gas WG in the front stage of the compressor 37, the composition of the gas introduced into the membrane separation device 30 is stabilized, and the suction pressure of the compressor 37 is stabilized. I can do it.
ここで、前記のごとく構成した装置で酸素富化ガスを採
取する実験を行った結果を説明する。Here, the results of an experiment in which oxygen-enriched gas was collected using the apparatus configured as described above will be explained.
まず、圧力変動吸着分離装置１０の各吸着塔１１ａ、ｌ
ｌｂ、ｌｌｃには、ゼオライト５Ａ（東ソー■製）を充
填し、前記吸着、洗浄、脱着の各工程の切換え時間は３
分とした。また、膜分離装置３０の分離膜３１には、酸
素と窒素の透過係数比（ＰＯ２／ＰＮ２）が３．５の高
分子膜を用いた。さらに、原料空気ＧＡは、乾燥剤と合
成ゼオライト１３Ｘを積層充填した吸着塔を切替え使用
する前処理装置１２に導入し、該原料空気ＧＡ中の水分
を１０ｐｐｍ、炭酸ガスを１０ｐｐｍ以下まで除去した
。First, each adsorption tower 11a, l of the pressure fluctuation adsorption separation device 10
lb and llc are filled with zeolite 5A (manufactured by Tosoh ■), and the switching time for each of the adsorption, washing, and desorption steps is 3.
It was a minute. Further, as the separation membrane 31 of the membrane separation device 30, a polymer membrane having an oxygen to nitrogen permeability coefficient ratio (PO2/PN2) of 3.5 was used. Furthermore, the raw air GA was introduced into a pretreatment device 12 that alternately uses an adsorption tower filled with a desiccant and synthetic zeolite 13X, and the moisture and carbon dioxide in the raw air GA were removed to 10 ppm or less.
そして上記前処理装置１２で精製した原料空気ＧＡ （
１０００Ｎ）／ｈ）を、脱着１回収の完了した第１吸着
塔１１ａに導入し、塔内圧力を０．２ｋｇ ／ ａｔ
Ｇまで昇圧した。該第１吸着塔１１ａが吸着工程を終了
した後、第２塔１１ｂから脱着回収されている純度９９
．９９５％の窒素を、回収タンク１６から洗浄ガスＦＧ
としてブロワ−１７により０ 、 ３ ｋｇ ／ ｃ＆
Ｇに昇圧し、第１吸着塔１１ａに導入して塔内の洗浄
を行った。この時、該第１吸着塔１１ａから排出された
洗浄排ガスＷＧ（５３２ＮＪ／ｈ）の酸素濃度は約３９
．４％であり、水分は１０ｐｐｍ以下、炭酸ガスも１０
ｐｐｍ以下であった。Then, the raw material air GA (
1000 N)/h) was introduced into the first adsorption tower 11a where desorption and recovery had been completed, and the pressure inside the tower was set to 0.2 kg/at.
Pressure increased to G. After the first adsorption tower 11a completes the adsorption step, the purity 99 is desorbed and recovered from the second tower 11b.
．． 995% of nitrogen is removed from the recovery tank 16 by cleaning gas FG.
0.3 kg/c& by blower 17 as
The pressure was raised to G and introduced into the first adsorption tower 11a to clean the inside of the tower. At this time, the oxygen concentration of the cleaning exhaust gas WG (532 NJ/h) discharged from the first adsorption tower 11a is approximately 39
．． 4%, water content is less than 10 ppm, and carbon dioxide gas is less than 10 ppm.
It was less than ppm.
次に、この洗浄排ガスＷＧを膜分離装置３０に導入して
酸素を濃縮し、酸素富化ガスＧｏ （２６６！ｌ／ｈ）
を得た。得られた酸素富化ガスＧＯの酸素濃度は約５３
，８％であり、水分、炭酸ガスは、いずれも１０ｐｐｍ
以下であった。残り２６６Ｎ！／ｈは、前記圧力変動吸
着分離装置１０の前処理塔の再生ガスとして用いた。Next, this washed exhaust gas WG is introduced into the membrane separator 30 to concentrate oxygen, and the oxygen-enriched gas Go (266!l/h) is
I got it. The oxygen concentration of the obtained oxygen-enriched gas GO is approximately 53
, 8%, and moisture and carbon dioxide are both 10 ppm.
It was below. 266N remaining! /h was used as a regeneration gas for the pretreatment tower of the pressure fluctuation adsorption separation device 10.
また、前記圧力変動吸着分離装置１０からは、純度９．
９．９９５％の製品高純度窒素ＰＮが５３２Ｎノ／ｈ得
られた。Further, the purity of the pressure fluctuation adsorption separation device 10 is 9.
Product high purity nitrogen PN of 9.995% was obtained at 532 N/h.
以上説明したように、本発明の酸素の濃縮方法は、天然
又は合成ゼオライトを吸着剤に使用した窒素採取用の圧
力変動吸着分離装置から排出される洗浄排ガスを原料ガ
スとして膜分離装置に供給するから、水分、炭酸ガスの
含有量が極めて少ない酸素富化ガスを容易に得ることが
できる。また上記洗浄排ガスは、その酸素濃度が空気の
約２倍に濃縮されているため、膜分離装置１段のみで５
０％以上の濃縮酸素を得ることができた。As explained above, in the oxygen concentration method of the present invention, the cleaning exhaust gas discharged from a pressure fluctuation adsorption separation device for nitrogen collection using natural or synthetic zeolite as an adsorbent is supplied as a raw material gas to a membrane separation device. From this, oxygen-enriched gas with extremely low moisture and carbon dioxide contents can be easily obtained. In addition, the oxygen concentration of the cleaning exhaust gas is approximately twice that of air, so only one stage of membrane separation equipment can
It was possible to obtain concentrated oxygen of 0% or more.
さらに、膜分離装置からの排ガスを、圧力変動吸着分離
装置の前処理装置の吸着塔を再生する再生ガスに用いる
ことにより、該前処理装置の再生用に他のガスを用意す
る必要がなくなり、運転コストを低減できる。Furthermore, by using the exhaust gas from the membrane separation device as the regeneration gas for regenerating the adsorption tower of the pretreatment device of the pressure fluctuation adsorption separation device, there is no need to prepare other gas for regeneration of the pretreatment device. Operation costs can be reduced.
図は本発明の一実施例を示す系統図である。
１０・・・圧力変動吸着分離装置 １１ａ１．１ｂ、
ｌｌｃ・・・吸着塔 １２・・・前処理装置３０・
・・膜分離装置 ３１・・・分離膜 ３７・・・圧
縮機 ＧＯ・・・酸素富化ガス ＰＮ・・・製品高
純度窒素 ＷＧ・・・洗浄排ガスThe figure is a system diagram showing one embodiment of the present invention. 10... Pressure fluctuation adsorption separation device 11a1.1b,
llc...Adsorption tower 12...Pretreatment device 30.
...Membrane separation device 31...Separation membrane 37...Compressor GO...Oxygen enriched gas PN...Product high purity nitrogen WG...Cleaning exhaust gas
Claims (1)
おいて、天然又は合成ゼオライトを吸着剤に使用して原
料空気から窒素を回収する圧力変動吸着分離装置の後段
に酸素富化膜を設けた膜分離装置を配設し、前記圧力変
動吸着分離装置から排出される洗浄排ガスを所定圧力に
昇圧して前記膜分離装置に供給することを特徴とする酸
素の濃縮方法。 ２、前記膜分離装置から排出される排ガスを、前記圧力
変動吸着分離装置に供給する原料空気の前処理を行う前
処理装置の吸着塔を再生する再生ガスに用いることを特
徴とする請求項１記載の酸素の濃縮方法。[Claims] 1. In a method for concentrating oxygen in air using air as a raw material, oxygen is added to the downstream stage of a pressure fluctuation adsorption separation device that uses natural or synthetic zeolite as an adsorbent to recover nitrogen from raw air. A method for concentrating oxygen, characterized in that a membrane separation device provided with an enrichment membrane is provided, and the washed exhaust gas discharged from the pressure fluctuation adsorption separation device is pressurized to a predetermined pressure and then supplied to the membrane separation device. 2. Claim 1, characterized in that the exhaust gas discharged from the membrane separation device is used as a regeneration gas for regenerating an adsorption tower of a pretreatment device that pretreats the feed air supplied to the pressure fluctuation adsorption separation device. Method for concentrating oxygen as described.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1145686A JPH0312307A (en) | 1989-06-08 | 1989-06-08 | Method for enriching oxygen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1145686A JPH0312307A (en) | 1989-06-08 | 1989-06-08 | Method for enriching oxygen |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0312307A true JPH0312307A (en) | 1991-01-21 |
Family
ID=15390748
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1145686A Pending JPH0312307A (en) | 1989-06-08 | 1989-06-08 | Method for enriching oxygen |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0312307A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5447559A (en) * | 1989-11-14 | 1995-09-05 | Air Products And Chemicals, Inc. | Hydrogen recovery by adsorbent membranes |
| WO2006013918A1 (en) * | 2004-08-05 | 2006-02-09 | Sumitomo Seika Chemicals Co., Ltd. | Double separation method and double separation system for oxygen gas and nitrogen gas |
| KR100698168B1 (en) * | 2000-09-18 | 2007-03-22 | 엘지전자 주식회사 | Oxygen Generator |
| JP5027662B2 (en) * | 2005-08-22 | 2012-09-19 | 住友精化株式会社 | Method and system for parallel separation of oxygen gas and nitrogen gas |
| WO2015197418A1 (en) * | 2014-06-25 | 2015-12-30 | Krinner Drucklufttechnik Gmbh | Air preparation method and device with a carbon dioxide adsorption and oxygen enrichment process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58151304A (en) * | 1982-02-27 | 1983-09-08 | Nippon Sanso Kk | Production of oxygen by pressure swing method |
| JPH01252502A (en) * | 1988-04-01 | 1989-10-09 | Hakko Seisakusho:Kk | Production of high-purity oxygen gas |
-
1989
- 1989-06-08 JP JP1145686A patent/JPH0312307A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58151304A (en) * | 1982-02-27 | 1983-09-08 | Nippon Sanso Kk | Production of oxygen by pressure swing method |
| JPH01252502A (en) * | 1988-04-01 | 1989-10-09 | Hakko Seisakusho:Kk | Production of high-purity oxygen gas |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5447559A (en) * | 1989-11-14 | 1995-09-05 | Air Products And Chemicals, Inc. | Hydrogen recovery by adsorbent membranes |
| KR100698168B1 (en) * | 2000-09-18 | 2007-03-22 | 엘지전자 주식회사 | Oxygen Generator |
| WO2006013918A1 (en) * | 2004-08-05 | 2006-02-09 | Sumitomo Seika Chemicals Co., Ltd. | Double separation method and double separation system for oxygen gas and nitrogen gas |
| JP2006043599A (en) * | 2004-08-05 | 2006-02-16 | Sumitomo Seika Chem Co Ltd | Method and system for parallel separation of oxygen gas and nitrogen gas |
| JP4538275B2 (en) * | 2004-08-05 | 2010-09-08 | 住友精化株式会社 | Method and system for parallel separation of oxygen gas and nitrogen gas |
| KR101120992B1 (en) * | 2004-08-05 | 2012-06-13 | 스미토모 세이카 가부시키가이샤 | Double separation method and double separation system for oxygen gas and nitrogen gas |
| JP5027662B2 (en) * | 2005-08-22 | 2012-09-19 | 住友精化株式会社 | Method and system for parallel separation of oxygen gas and nitrogen gas |
| WO2015197418A1 (en) * | 2014-06-25 | 2015-12-30 | Krinner Drucklufttechnik Gmbh | Air preparation method and device with a carbon dioxide adsorption and oxygen enrichment process |
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