JPS6155029B2 - - Google Patents
Info
- Publication number
- JPS6155029B2 JPS6155029B2 JP53120361A JP12036178A JPS6155029B2 JP S6155029 B2 JPS6155029 B2 JP S6155029B2 JP 53120361 A JP53120361 A JP 53120361A JP 12036178 A JP12036178 A JP 12036178A JP S6155029 B2 JPS6155029 B2 JP S6155029B2
- Authority
- JP
- Japan
- Prior art keywords
- heat exchanger
- oxygen
- waste gas
- air
- temperature
- 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
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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
-
- 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
- F25J3/04151—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
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
-
- 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
- F25J3/0423—Subcooling of liquid process streams
-
- 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
- F25J3/04309—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 nitrogen
- F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
-
- 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
- F25J3/044—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 single pressure main column system only
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
【発明の詳細な説明】
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高圧酸素を採取す
る空気分離方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention compresses raw air taken from the atmosphere.
This invention relates to an air separation method that collects high-pressure oxygen through dehumidification, cooling, and rectification separation.
空気分離装置においては、原料空気中に含まれ
るアセチレン等の炭化水素の爆発に対処するた
め、シリカゲル等を充填した吸着器を、液体空気
または液体酸素ラインに設置して炭化水素を吸着
させ、約１週間の周期で切替再生が行なわれる。
吸着器の切替再生は繁雑な運転が必要となる。 In air separation equipment, in order to deal with the explosion of hydrocarbons such as acetylene contained in the feed air, an adsorber filled with silica gel etc. is installed in the liquid air or liquid oxygen line to adsorb hydrocarbons. Switching reproduction is performed at a cycle of one week.
Switching regeneration of adsorbers requires complicated operation.
従来の単式精留塔の構造を第１図に示す。この
場合、リボイラー９はアルミプレート式熱交換器
または直管式熱交換器を使用し、液化した空気は
精留塔８の塔底で受け、塔底のノズルより取出し
て過冷却器１０を経て精留塔８の上部に送り込む
ようになつている。しかして、従来の型式のリボ
イラー９では、塔底の液体空気は飽和温度以下に
過冷却することはできない。また、液体酸素は液
酸ポンプ１１より炭化水素を吸着除去する吸着器
（図示せず）を経て取出される。 The structure of a conventional single rectification column is shown in Figure 1. In this case, the reboiler 9 uses an aluminum plate heat exchanger or a straight tube heat exchanger, and the liquefied air is received at the bottom of the rectification column 8, taken out from the nozzle at the bottom, and passed through the subcooler 10. It is designed to be sent to the upper part of the rectification column 8. Thus, in the conventional type of reboiler 9, the liquid air at the bottom of the column cannot be supercooled below the saturation temperature. Further, liquid oxygen is taken out from the liquid acid pump 11 via an adsorber (not shown) that adsorbs and removes hydrocarbons.
本発明の目的は、切替再生の繁雑な吸着器を不
要とし、かつ、炭化水素の爆発を防止することに
ある。 An object of the present invention is to eliminate the need for an adsorption device that requires complicated switching and regeneration, and to prevent explosions of hydrocarbons.
本発明の他の目的は、リボイラーにおける熱交
換量を増加させて酸素の回収率を増大させること
にある。 Another object of the present invention is to increase the rate of oxygen recovery by increasing the amount of heat exchange in the reboiler.
本発明の要点は、酸素熱交換器としてコイル式
熱交換器を使用し、管内側に約150Kg/cm2Gの液体
酸素を送入してガス化および常温までの温度回復
を行なわせると共に、リボイラーとしてコイル式
熱交換器を使用し、管内側に原料空気を送入して
液化させた後、更に過冷却してリボイラーにおけ
る熱交換量を増大させ、精留塔の上昇ガス量およ
び環流液量を増加させることにある。 The main point of the present invention is to use a coil type heat exchanger as an oxygen heat exchanger, to feed approximately 150 kg/cm 2 G of liquid oxygen into the inside of the tube to perform gasification and temperature recovery to room temperature. A coil-type heat exchanger is used as a reboiler, and after feeding raw air into the tube and liquefying it, it is further supercooled to increase the amount of heat exchange in the reboiler. The goal is to increase the amount.
液体酸素は、約150Kg/cm2Gの高圧とすることに
より、酸素ガス中のアセチレンの分圧が高く、ア
セチレンが液体酸素中に蓄積することはないが、
酸素熱交換器の酸素側通路が複雑な構造である
と、アセチレンが局部的に蓄積する可能性があ
る。本発明は、酸素熱交換器にコイル式熱交換器
を用いて、酸素を円滑な管内側に通すことによ
り、アセチレンの局部的な蓄積をなくして、安全
な運転を行わせるようにしたものである。 By applying liquid oxygen to a high pressure of approximately 150 kg/cm 2 G, the partial pressure of acetylene in the oxygen gas is high, and acetylene does not accumulate in liquid oxygen.
If the oxygen side passage of the oxygen heat exchanger has a complicated structure, acetylene may accumulate locally. The present invention uses a coil type heat exchanger as an oxygen heat exchanger to allow oxygen to pass through the smooth inside of the tube, thereby eliminating local accumulation of acetylene and ensuring safe operation. be.
本発明の一実施例を第２図によつて説明する。
第２図は空気分離装置の原料空気圧縮機１、脱湿
塔４、廃ガス熱交換器５、コイル式熱交換器より
なる酸素熱交換器６、液化器７、精留塔８、液酸
ポンプ１１、膨脹タービン１３の系統図を示した
ものである。 An embodiment of the present invention will be described with reference to FIG.
Figure 2 shows the raw air compressor 1, dehumidification tower 4, waste gas heat exchanger 5, oxygen heat exchanger 6 consisting of a coil heat exchanger, liquefier 7, rectification tower 8, and liquid acid of the air separation equipment. A system diagram of the pump 11 and the expansion turbine 13 is shown.
大気から取入れた原料空気を原料空気圧縮機１
で約30Kg/cm2Gに圧縮し、アフタークーラー２で
約40℃まで冷却し、更にフレオン冷却器３で約５
℃まで冷却し、脱湿塔４で水分および炭酸ガスを
除去した後、原料空気を２分して、その一部は廃
ガス熱交換器５で廃ガスと熱交換させて約−140
℃まで冷却し、他の一部はコイル式の酸素熱交換
器６で高圧液体酸素と熱交換させて約−140℃ま
で冷却して再び合流させる。合流した原料空気
は、液化器７で廃ガスと熱交換させて約−145℃
まで冷却し、原料空気の一部を液化させ、単式精
留塔８の下部に設置されたリボイラー９で液体酸
素と熱交換して全量液化され、さらに約−150℃
まで過冷却され、過冷却器１０で廃ガスと熱交換
して約−155℃まで過冷却されて、精留塔８の上
部に送入される。 Raw air compressor 1 uses raw air taken in from the atmosphere.
compressed to approximately 30Kg/cm 2 G, cooled to approximately 40℃ in aftercooler 2, and further compressed to approximately 5Kg/cm 2 G in Freon cooler 3.
After cooling to ℃ and removing moisture and carbon dioxide in the dehumidification tower 4, the raw air is divided into two parts, and a part of it is heat exchanged with the waste gas in the waste gas heat exchanger 5 to reduce the temperature to about -140℃.
The other part is cooled to about -140°C by exchanging heat with high-pressure liquid oxygen in a coil-type oxygen heat exchanger 6, and then recombined. The combined raw air is heated to approximately -145°C by exchanging heat with the waste gas in the liquefier 7.
The raw air is cooled to a temperature of approximately -150°C, and a portion of the raw air is liquefied, and the entire amount is liquefied by heat exchange with liquid oxygen in the reboiler 9 installed at the bottom of the single rectification column 8.
It is supercooled to about -155° C. by exchanging heat with the waste gas in the supercooler 10, and then sent to the upper part of the rectification column 8.
精留塔８で分離された液体酸素は、精留塔８の
底部より取出され、液酸ポンプ１１で約150Kg/cm2
Ｇに昇圧され、酸素熱交換器６の管内側を通り原
料空気と熱交換してガス化し、常温まで温度回復
して導管１２から高圧酸素ガスが製品として採取
される。 The liquid oxygen separated in the rectification column 8 is taken out from the bottom of the rectification column 8, and is pumped with a liquid acid pump 11 at approximately 150Kg/cm 2
The oxygen gas is pressurized to G, passes through the inside of the tube of the oxygen heat exchanger 6, exchanges heat with the raw material air, and is gasified.The temperature is then recovered to room temperature, and high-pressure oxygen gas is collected from the conduit 12 as a product.
精留塔８上部から取出された廃ガスは、液化器
７で約−140℃まで温度上昇され、膨脹タービン
１３で約８Kg/cm2Gから約0.5Kg/cm2Gに膨脹された
寒冷発生した後、過冷却器１０で約−150℃まで
温度上昇し、更に廃ガス熱交換器５で常温まで温
度回復して導管１４から大気放出される。 The waste gas taken out from the upper part of the rectification column 8 is heated to about -140℃ in the liquefier 7, and expanded from about 8Kg/cm 2 G to about 0.5Kg/cm 2 G in the expansion turbine 13. After that, the temperature is raised to about -150°C in the supercooler 10, and then the temperature is recovered to room temperature in the waste gas heat exchanger 5, and then released into the atmosphere through the conduit 14.
本発明は以上述べたようにコイル式熱交換器よ
りなる酸素熱交換器の円滑な管内側に高圧の液体
酸素を通し、管内で高圧の液体酸素を蒸発させる
ようにしたものであるから、吸着器を必要とせず
炭化水素の局部的積積を防止することができ、炭
化水素の爆発の危険性を未然に防止して安全な運
転を行なわせることができると同時に高圧の酸素
ガスを得ることができ、かつ、リボイラーとして
コイル式熱交換器を使用したものであるから、原
料空気を液化し、さらに飽和温度以下に過冷却す
ることができ、リボイラーにおける熱交換量を増
大して精留が容易となり、酸素の回収率を増大さ
せることができる。 As described above, the present invention passes high-pressure liquid oxygen inside the smooth tubes of an oxygen heat exchanger consisting of a coil type heat exchanger, and evaporates the high-pressure liquid oxygen within the tubes. To prevent local accumulation of hydrocarbons without the need for a container, to prevent the danger of explosion of hydrocarbons and to ensure safe operation, and to obtain high-pressure oxygen gas at the same time. Moreover, since it uses a coil heat exchanger as a reboiler, it is possible to liquefy the raw air and further subcool it below the saturation temperature, increasing the amount of heat exchange in the reboiler and improving rectification. This makes it possible to increase the recovery rate of oxygen.
第１図は従来の単式精留塔の構造を示す略図、
第２図は本発明による空気分離装置の一実施例を
示す系統図である。
１′……原料空気圧縮機、２……アフタークー
ラー、３……フレオン冷却器、４……脱湿塔、５
……廃ガス熱交換器、６……酸素熱交換器、７…
…液化器、８……精留塔、９……リボイラー、１
０……過冷却器、１１……液酸ポンプ、１２，１
４……導管、１３……膨脹タービン。
Figure 1 is a schematic diagram showing the structure of a conventional single rectification column.
FIG. 2 is a system diagram showing an embodiment of the air separation apparatus according to the present invention. 1'... Raw air compressor, 2... Aftercooler, 3... Freon cooler, 4... Dehumidification tower, 5
...Waste gas heat exchanger, 6...Oxygen heat exchanger, 7...
...Liquifier, 8...Rectification column, 9...Reboiler, 1
0...supercooler, 11...liquid acid pump, 12,1
4... Conduit, 13... Expansion turbine.
Claims (1)
去した後２分し、その一部を廃ガス熱交換器で廃
ガスと熱交換させて冷却し、他の一部をコイル式
熱交換器よりなる酸素熱交換器で高圧酸素と熱交
換させて冷却し、再び原料空気を合流させて液化
器で原料空気の一部を液化させた後、単式精留塔
の下部に設置されたリボイラーで原料空気を全量
液化させ、過冷却器で過冷却して精留塔上塔に送
入し、精留塔上部から出た廃ガスを液化器で温度
上昇させた後、膨張タービンで膨張させて寒冷を
発生させ、過冷却器および廃ガス熱交換器で常温
まで温度回復させた後大気放出し、精留塔下部か
ら出た液体酸素を液酸ポンプで昇圧し、酸素熱交
換器の管内側を通して温度回復させた後、高圧酸
素ガスを製品として採取することを特徴とする高
圧酸素を採取する空気分離方法。1 The raw air is compressed, water and carbon dioxide are removed, and then divided into two parts. Part of it is cooled by exchanging heat with waste gas in a waste gas heat exchanger, and the other part is cooled by a coil heat exchanger. The raw air is cooled by exchanging heat with high-pressure oxygen in an oxygen heat exchanger, and then the raw air is combined again and a part of the raw air is liquefied in a liquefier. The entire amount of air is liquefied, supercooled in a supercooler, and sent to the upper tower of the rectification tower.The temperature of the waste gas coming out of the upper part of the rectification tower is raised in the liquefier, and then expanded in an expansion turbine to cool it. After recovering the temperature to room temperature in a supercooler and waste gas heat exchanger, it is released into the atmosphere. The liquid oxygen coming out from the bottom of the rectification column is pressurized by a liquid acid pump and passed through the inside of the tube of the oxygen heat exchanger. An air separation method for collecting high-pressure oxygen, which is characterized by collecting high-pressure oxygen gas as a product after temperature recovery.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12036178A JPS5549681A (en) | 1978-10-02 | 1978-10-02 | Air separator for obtaining highhpressure oxygen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12036178A JPS5549681A (en) | 1978-10-02 | 1978-10-02 | Air separator for obtaining highhpressure oxygen |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5549681A JPS5549681A (en) | 1980-04-10 |
| JPS6155029B2 true JPS6155029B2 (en) | 1986-11-26 |
Family
ID=14784286
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP12036178A Granted JPS5549681A (en) | 1978-10-02 | 1978-10-02 | Air separator for obtaining highhpressure oxygen |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5549681A (en) |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1501722A1 (en) * | 1966-01-13 | 1969-06-26 | Linde Ag | Process for cryogenic air separation for the production of highly compressed gaseous and / or liquid oxygen |
| JPS5439830B2 (en) * | 1974-05-04 | 1979-11-30 |
-
1978
- 1978-10-02 JP JP12036178A patent/JPS5549681A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5549681A (en) | 1980-04-10 |
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