JPH02279979A - Air separation method and its device - Google Patents

Air separation method and its device

Info

Publication number
JPH02279979A
JPH02279979A JP10005589A JP10005589A JPH02279979A JP H02279979 A JPH02279979 A JP H02279979A JP 10005589 A JP10005589 A JP 10005589A JP 10005589 A JP10005589 A JP 10005589A JP H02279979 A JPH02279979 A JP H02279979A
Authority
JP
Japan
Prior art keywords
air
heat exchanger
cooled
compressor
cool
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
Application number
JP10005589A
Other languages
Japanese (ja)
Inventor
Hisazumi Ishizu
石津　尚澄
Junichi Hosokawa
純一 細川
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hitachi Ltd
Original Assignee
Hitachi Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Hitachi Ltd filed Critical Hitachi Ltd
Priority to JP10005589A priority Critical patent/JPH02279979A/en
Publication of JPH02279979A publication Critical patent/JPH02279979A/en
Pending legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

PURPOSE:To allow the device to lessen pressure loss by passage resistance of a heat exchanger to enlarge an expansion ratio of an expansion turbine so as to enlarge a cold heat production quantity by providing an air precooler at the outlet of an after-cooler of a compressor and allowing the device to cool feed air by product oxygen allowed to flow out from the air heat exchanger to allow the feed air to flow in the air heat exchanger so as to send in the expansion turbine. CONSTITUTION:After feed air is compressed in a feed air compressor 1 to cool by an after- cooler 2 to heat-exchange with Freon in an air cooler 3 to cool so as to remove moisture, the feed air is allowed to adsorb and remove moisture and carbon dioxide in a desulfurizer 5 to obtain dry air. The feed air of the outlet of the desulfurizer 5 is divided into two halves, a half thereof is cooled in an air heat exchanger 7 to send in a fractionator 8. The other half is guided in the inlet of a compressor 10 joined to an expansion turbine 11 and after it is compressed by the compressor 10, allowed to heat-exchange with cooling water in an after-cooler 12 to cool. After the feed air is guided to an air precooler 15 and allowed to heat-exchange with product oxygen allowed to flow out from the air heat exchanger 7 to cool, it is guided to the air heat exchanger 7 to cool to extract and allowed to perform adiabatic expansion with the use of the expansion turbine 11 to produce cold heat so as to send into the fractionator 8.

Description

【発明の詳細な説明】 〔産業上の利用分野〕 本発明は大気から取入れた原料空気を圧縮、脱湿、冷却
および精留分離して、酸素、窒素、アルゴン等の分離生
成物を採取する空気分離装置に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention compresses, dehumidifies, cools, and rectifies raw air taken from the atmosphere to collect separated products such as oxygen, nitrogen, and argon. It relates to air separation equipment.

〔従来の技術〕[Conventional technology]

従来の空気分離装置な第２図により説明する。 A conventional air separation device will be explained with reference to FIG.

因において、大気から取入れた原料空気を原料空気圧縮
機ｌで約５Ｋｇ／ＣＩＩＧに圧縮し、アフタクーラー２
で約４０℃に冷却した後更に空気冷却器３で約５℃まで
冷却して水滴分離器４で水分を除去した後、脱湿塔５で
水分および炭酸ガスな吸着除去して約８℃の乾燥空気を
得る。この乾燥された原料空気を空気熱交７に送入して
冷却し、約−１００℃の空気と約−１７０℃の空気に２
分流する。約−１００℃の空気はタービン熱交９で約３
６℃まで昇温させ、膨張タービン１１と結合された圧縮
機１０で約７　Ｋｐ　／　ａ／Ｉ　Ｇに昇圧した後アフ
タークーラー１２で約４０℃に冷却し空気熱交９で約−
９６℃まで冷却して、膨張タービン１１で膨張させて精
留塔８に送入される。精留塔８で分離された酸素および
窒素は空気熱交７で約４℃まで昇温されおのおの導管１
３および１４より取出される。精留塔８から出た廃ガス
の一部は再生加熱器６で約２００℃に加熱されて脱湿塔
５の加熱再生に使用される。なお、この種の装置として
関連するものには例えば特開昭５５−１５０４７２号等
が挙げられる。In this case, the raw air taken in from the atmosphere is compressed to about 5 kg/CIIG by the raw air compressor 1, and the aftercooler 2
After being cooled to about 40°C in the air cooler 3, it is further cooled down to about 5°C, water is removed in the water droplet separator 4, water and carbon dioxide are adsorbed and removed in the dehumidification tower 5, and the temperature is about 8°C. Get dry air. This dried raw material air is sent to the air heat exchanger 7 and cooled, and is divided into air at approximately -100°C and air at approximately -170°C.
Divert. Air at about -100℃ is heated to about 3 by the turbine heat exchanger 9.
The temperature is raised to 6°C, and the pressure is increased to approximately 7 Kp/a/I G by a compressor 10 coupled to an expansion turbine 11, and then cooled to approximately 40°C by an aftercooler 12, and then reduced to approximately - by an air heat exchanger 9.
It is cooled to 96° C., expanded by an expansion turbine 11, and sent to a rectification column 8. Oxygen and nitrogen separated in the rectification column 8 are heated to approximately 4°C in an air heat exchanger 7, and then passed through each conduit 1.
3 and 14. A part of the waste gas discharged from the rectification column 8 is heated to about 200° C. by the regeneration heater 6 and used for heating and regeneration in the dehumidification column 5. Incidentally, related devices of this type include, for example, Japanese Patent Application Laid-open No. 150472/1983.

〔発明が解決しようとする課題〕[Problem to be solved by the invention]

上記従来技術は、脱湿塔を出た原料空気の温度は約８℃
であるため、空気熱交に入る原料空気は約８℃と低いの
に対し、圧縮機のアフタークーラーでは原料空気が冷却
水と熱交換されて冷却されるためアフタークーラーの出
口温度は約４０℃と高くなり、空気熱交に入れることは
不可能であった。このため空気熱交と別にタービン熱交
を設けて、原料空気を約４０℃から約−９６°Ｃまで冷
却させる必要があった。原料空気は空気熱交およびター
ビン熱交を通って圧縮機に入るためこれらの熱交の流路
抵抗による圧力損失が生じ、圧縮機の入口圧力が低くな
るという欠点があった。圧縮機の入口圧力が低くなるこ
とにより出口圧力が低くなり、膨張タービンの入口圧力
が低くなって膨張タービンの膨張比が小さくなり、寒冷
発生１ががさくなるという欠点があった。In the above conventional technology, the temperature of the raw air leaving the dehumidification tower is approximately 8°C.
Therefore, the feed air that enters the air heat exchanger is as low as about 8 degrees Celsius, whereas in the aftercooler of the compressor, the feed air is cooled by heat exchange with the cooling water, so the aftercooler outlet temperature is about 40 degrees Celsius. It became so high that it was impossible to put it into an air heat exchanger. Therefore, it was necessary to provide a turbine heat exchanger in addition to the air heat exchanger to cool the feed air from about 40°C to about -96°C. Since raw air enters the compressor through an air heat exchanger and a turbine heat exchanger, a pressure loss occurs due to the flow path resistance of these heat exchangers, resulting in a disadvantage that the inlet pressure of the compressor becomes low. As the inlet pressure of the compressor is lowered, the outlet pressure is lowered, and the inlet pressure of the expansion turbine is lowered, resulting in a lower expansion ratio of the expansion turbine and a disadvantage in that the cold generation 1 is increased.

本究明の目的は、熱交の流路抵抗による圧力損失を小さ
くし、膨張タービンの膨張比を大きくし、寒冷光生量を
大きくできる空気分離装置を提供することにある。The purpose of this research is to provide an air separation device that can reduce pressure loss due to heat exchange flow path resistance, increase the expansion ratio of an expansion turbine, and increase the amount of cold light produced.

本発明の他の目的は、タービン熱交が省略できる安価な
空気分離装置を提供することにある。Another object of the present invention is to provide an inexpensive air separation device in which turbine heat exchange can be omitted.

〔課題を解決するための手段〕[Means to solve the problem]

３　。 3.

４　・ 上記目的を達成するために、圧縮機のアフタークーラー
の出口に空気予冷器を設け、空気熱交から出た約４℃の
製品酸素で原料空気を約８℃まで冷却し、空気熱交に入
れて約−９６℃で膨張タービンに送入する。4. In order to achieve the above purpose, an air precooler is installed at the outlet of the aftercooler of the compressor, and the feed air is cooled to about 8°C with product oxygen at about 4°C from the air heat exchanger. and fed into an expansion turbine at about -96°C.

空気熱交の出口の製品酸素は約４℃であり、アフターク
ーラーの出口の原料空気を約４０℃から約８℃まで冷却
することができるので、従来のタービン熱交は不要とす
ることができる。The product oxygen at the outlet of the air heat exchanger is about 4°C, and the raw air at the outlet of the aftercooler can be cooled from about 40°C to about 8°C, so the conventional turbine heat exchanger can be dispensed with. .

〔作　　　用〕[For production]

従来のタービン熱交が不要となるので、脱湿塔を出た原
料空気は直接導管で圧縮機に送入することができるので
、圧縮機の人口圧力を高くすることができる。圧縮機の
アフタークーラーを出た原料空気は空気予冷器で約４０
℃から約８℃まで冷却し空気熱交に送入することができ
る。Since the conventional turbine heat exchanger is not required, the feed air leaving the dehumidification tower can be directly conduited to the compressor, thereby increasing the compressor's artificial pressure. The raw air that exits the aftercooler of the compressor is heated to approximately 40% by air precooler.
It can be cooled from 0.degree. C. to about 8.degree. C. and fed into an air heat exchanger.

〔実　施　例〕〔Example〕

以下、本発明の一実施例を第１図により説明する。本図
は原料空気圧縮機１．空気冷却器３．脱湿塔５．空気熱
交７、膨張タービン１１．圧縮機１０゜空気予冷器１５
．精留塔８等からなる空気分離装置の系統図を示したも
のである。An embodiment of the present invention will be described below with reference to FIG. This diagram shows raw air compressor 1. Air cooler 3. Dehumidification tower5. Air heat exchanger 7, expansion turbine 11. Compressor 10° Air precooler 15
．． A system diagram of an air separation device including a rectification column 8 and the like is shown.

大気から取入れた原料空気を原料空気圧縮ｔｆｌＮで約
５に９／ｆｆ１Ｇに圧縮し、アフタークーラー２で約４
０℃に冷却した後更に空気冷却器３でフレオンと熱交換
させて約５℃まで冷却して、水滴分離器４で水分を除去
した後、脱湿塔５で水分および炭酸ガスを吸着除去して
約８℃の乾燥空気を得る。The raw air taken in from the atmosphere is compressed to about 5 to 9/ff1G by the raw air compressor tflN, and the aftercooler 2 compresses it to about 4
After cooling to 0°C, it is further cooled to about 5°C by heat exchange with Freon in an air cooler 3, and water is removed in a water droplet separator 4, and then water and carbon dioxide are adsorbed and removed in a dehumidification tower 5. to obtain dry air at approximately 8°C.

脱湿塔５の出口の原料空気を２分流に分け、１分流は空
気熱交７で約−１７０℃まで冷却して精留１？ｉ８に送
入する。他の１分流は膨張タービン１１と結合された圧
縮機１０の入口に導き、圧縮９．１０で約８　Ｋ５＋　
／　６Ｊ、　Ｇに昇圧した後アフタークーラー１２で冷
却水と熱交換させて約４０℃まで冷却する。この約４０
℃の原料空気を空気予冷器１５に導き、空気熱交７を出
た約４℃の製品酸素と熱交換させ約８℃まで冷却した後
、空気熱交７に導き約−９６℃まで冷却して抜出し、膨
張タービン１１で断熱膨張させ寒冷を発生させ精留塔８
に送入する。The raw air at the outlet of the dehumidification tower 5 is divided into two streams, and one branch is cooled to approximately -170°C in an air heat exchanger 7 to undergo rectification 1? Send it to i8. The other branch is led to the inlet of the compressor 10 coupled to the expansion turbine 11 and has a compression rate of about 8 K5+ at 9.10.
/ After increasing the pressure to 6J, G, the aftercooler 12 exchanges heat with cooling water and cools it to about 40°C. This approximately 40
℃ feed air is introduced into the air precooler 15, where it is heat-exchanged with the product oxygen at about 4℃ that exits the air heat exchanger 7, cooled to about 8℃, and then introduced into the air heat exchanger 7 and cooled to about -96℃. It is extracted and adiabatically expanded in the expansion turbine 11 to generate cold, and then sent to the rectification column 8.
Send to.

精留塔８で精留分離された製品酸素、製品窒素および廃
ガスは空気熱交７で原料空気と熱交換して約４℃まで温
度回復する。製品酸素は空気予冷器で約２２℃まで加熱
されて導管１３より取出される。製品窒素は約４℃のま
ま導管１４より取出される。廃ガスの一部は再生加熱器
６で約２００℃に加熱されて脱湿塔５の加熱再生に使用
される。The product oxygen, product nitrogen, and waste gas separated by rectification in the rectification column 8 exchange heat with raw air in the air heat exchanger 7 to recover the temperature to about 4°C. Product oxygen is heated to about 22° C. in an air precooler and taken out through conduit 13. Product nitrogen is taken out through conduit 14 while still at about 4°C. A part of the waste gas is heated to about 200° C. by the regeneration heater 6 and used for heating and regeneration in the dehumidification tower 5.

〔発明の効果〕〔Effect of the invention〕

本発明によれば、脱湿塔を出た原料空気が直接圧縮機に
導かれるので、圧力損失を小さ（することができ、圧縮
機の入口圧力、出口圧力および膨張タービンの人口圧力
を高くすることができ、膨張タービンにおける膨張比が
大きくなり、寒冷発生蓋を大きくすることができる。According to the present invention, since the feed air leaving the dehumidification tower is directly guided to the compressor, the pressure loss can be reduced, and the inlet pressure and outlet pressure of the compressor and the population pressure of the expansion turbine can be increased. This increases the expansion ratio in the expansion turbine, making it possible to increase the size of the cold generation lid.

さらに、従来のタービン熱交が不要となるので、設備費
も小さくすることができる。Furthermore, since conventional turbine heat exchange is not required, equipment costs can also be reduced.

【図面の簡単な説明】[Brief explanation of drawings]

第１図は本発明の一実施例の空気分離装置の系統図、第
２図は従来の空気分離装置の系統図である。 １・・・・・・原料空気圧縮機、５・・・・・・脱湿塔
、７・・・・・・空気熱交、８・・・・・ 膨張タービンFIG. 1 is a system diagram of an air separation device according to an embodiment of the present invention, and FIG. 2 is a system diagram of a conventional air separation device. 1... Raw air compressor, 5... Dehumidification tower, 7... Air heat exchanger, 8... Expansion turbine

Claims (1)

【特許請求の範囲】 １、大気から取入れた原料空気中の水分および炭酸ガス
を脱湿塔で吸着除去し空気熱交で冷却し精留塔で精留分
離する空気分離方法において、脱湿塔で水分および炭酸
ガスを除去した原料空気を二分流に分け、１分流は空気
熱交を通して精留塔に送入し、他の１分流は膨張タービ
ンと結合された圧縮機で昇圧した後、アフタークーラー
で冷却水と熱交換させて冷却し、更に空気予冷器で空気
熱交を出た製品酸素と熱交換させて冷却した後、空気熱
交で冷却して膨張タービンで膨張させ精留塔に送入する
ことを特徴とする空気分離方法。 ２、大気から取入れた原料空気中の水分および炭酸ガス
を脱湿塔で吸着除去し空気熱交で冷却し精留塔で精留分
離する空気分離装置において、前記脱湿塔が水分および
炭酸ガスを除去した原料空気を２分流し、１分流を空気
熱交を通して精留塔に導き、他の１分流を膨張タービン
と結合された圧縮機で昇圧後、アフタークーラーで冷却
し、さらに空気予冷器で冷却後、空気熱交で冷却して膨
張タービンで膨張させ精留塔に導くように構成したこと
を特徴とする空気分離装置。[Scope of Claims] 1. In an air separation method in which moisture and carbon dioxide in raw air taken in from the atmosphere are adsorbed and removed in a dehumidification tower, cooled by air heat exchange, and separated by rectification in a rectification tower, the dehumidification tower The feed air from which water and carbon dioxide have been removed is divided into two streams, one stream is sent to the rectification column through an air heat exchanger, and the other stream is pressurized by a compressor connected to an expansion turbine and then sent to the after-sales service. The product is cooled by exchanging heat with the cooling water in the cooler, and further cooled by exchanging heat with the product oxygen exiting the air heat exchanger in the air precooler, then cooled by the air heat exchanger, expanded by the expansion turbine, and sent to the rectification tower. An air separation method characterized in that: 2. In an air separation device in which moisture and carbon dioxide in the raw air taken in from the atmosphere are adsorbed and removed in a dehumidification tower, cooled by an air heat exchanger, and separated by rectification in a rectification tower, the dehumidification tower removes moisture and carbon dioxide. The raw air from which the 1. An air separation device characterized in that the air separation device is configured to be cooled by an air heat exchanger, expanded by an expansion turbine, and guided to a rectification column.
JP10005589A 1989-04-21 1989-04-21 Air separation method and its device Pending JPH02279979A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP10005589A JPH02279979A (en) 1989-04-21 1989-04-21 Air separation method and its device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP10005589A JPH02279979A (en) 1989-04-21 1989-04-21 Air separation method and its device

Publications (1)

Publication Number Publication Date
JPH02279979A true JPH02279979A (en) 1990-11-15

Family

ID=14263802

Family Applications (1)

Application Number Title Priority Date Filing Date
JP10005589A Pending JPH02279979A (en) 1989-04-21 1989-04-21 Air separation method and its device

Country Status (1)

Country Link
JP (1) JPH02279979A (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100768319B1 (en) * 2001-12-05 2007-10-17 주식회사 포스코 Operation method to prevent cold loss of air separation device

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS63143482A (en) * 1986-12-05 1988-06-15 株式会社日立製作所 TSA adsorption type air cryogenic separation equipment

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS63143482A (en) * 1986-12-05 1988-06-15 株式会社日立製作所 TSA adsorption type air cryogenic separation equipment

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100768319B1 (en) * 2001-12-05 2007-10-17 주식회사 포스코 Operation method to prevent cold loss of air separation device

Similar Documents

Publication Publication Date Title
JPS5939671B2 (en) Air separation method and device
GB2083193A (en) Air separating system
US4746343A (en) Method and apparatus for gas separation
US11137205B2 (en) Method and apparatus for eliminating heat bumps following regeneration of adsorbers in an air separation unit
KR20230132460A (en) Method and apparatus for drying carbon dioxide-rich flows
CN1169333A (en) All-low-pressure air separation technology
JPS5527034A (en) Pressure swing adsorption system used with heat regeneration method
JPH02118391A (en) Manufacturing device for liquid air
JPS54162678A (en) Air separating apparatus taking out liquid product utilizing coldness of lng
JP3304810B2 (en) Feed air dehumidification and cooling system in feed air multistage compressor
JP3305977B2 (en) Feed air dehumidification and cooling system in feed air multistage compressor
CN209917566U (en) Polyolefin exhaust gas recovery device
JPS5814808B2 (en) Dry oxygen enriched air production method
CN118681378B (en) High-efficient drying device of heating power
JPH0710226Y2 (en) Air liquefaction separation device
CN204421487U (en) Pure apparatus for producing liquid nitrogen
US20250237431A1 (en) Method and apparatus for compressing a gas
JPS62117613A (en) Dehumidification method and device
JP2551461B2 (en) Pretreatment method of raw material air in air separation device
CA2157826A1 (en) Air separation method and apparatus
JP3385409B2 (en) Air liquefaction separation method and apparatus
JPS6138391B2 (en)
CN210103456U (en) Industrial vacuum adsorption type oxygen generation equipment
JPS6044583B2 (en) Air separation method using cooling of liquefied natural gas
JPH03168583A (en) Method and apparatus for liquefying and separating air