JPS6044583B2 - Air separation method using cooling of liquefied natural gas - Google Patents
Air separation method using cooling of liquefied natural gasInfo
- Publication number
- JPS6044583B2 JPS6044583B2 JP3853377A JP3853377A JPS6044583B2 JP S6044583 B2 JPS6044583 B2 JP S6044583B2 JP 3853377 A JP3853377 A JP 3853377A JP 3853377 A JP3853377 A JP 3853377A JP S6044583 B2 JPS6044583 B2 JP S6044583B2
- Authority
- JP
- Japan
- Prior art keywords
- air
- heat exchanger
- nitrogen
- gas
- liquefied natural
- 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
- F25J3/044—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
- 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
- F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
-
- 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
- F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
- F25J3/0426—The cryogenic component does not participate in the fractionation
- F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
-
- 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
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
-
- 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
- F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
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)
Description
【発明の詳細な説明】
本発明は、液化天然ガスの寒冷を利用した空気分離方法
に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an air separation method using refrigeration of liquefied natural gas.
空気分離装置において、液化天然ガスの寒冷を利用する
方法としては、従来より液体酸素および液体窒素を採取
する液化回路付空気分離装置において、液化回路の窒素
または空気を液化天然ガスで冷却する方法、あるいは第
１図に示すように、原料空気を空気圧縮機２４で約５に
９／ｄＧに圧縮した後脱湿塔２で脱湿し、空気熱熱交換
器３で低温戻りガスと熱交換させて冷却した後導管１３
より精留塔４下塔に導入すると同時に、その一部を空気
熱交換器３中間より拙筆して膨脹タビーン２３に導入し
、寒冷を発生させて精留塔４上塔に導入するようにした
ものにおいて、空気圧縮機２４のインタークーラ２５に
導管２６より液化天然ガスを導入して原料空気を冷却す
る方法などがあるが、前者の方法はガス酸素およびガス
窒素を採取する場合には有効でなく、また、後者の方法
ではインタークーラ２５において原料空気中の水分およ
び炭酸ガスが氷結するという問題がある。In an air separation device, methods of utilizing the cold of liquefied natural gas include a method of cooling nitrogen or air in the liquefaction circuit with liquefied natural gas in an air separation device with a liquefaction circuit that collects liquid oxygen and liquid nitrogen; Alternatively, as shown in FIG. 1, raw air is compressed to approximately 5 to 9 dG by an air compressor 24, dehumidified by a dehumidification tower 2, and then heat exchanged with low-temperature return gas by an air-to-air heat exchanger 3. After cooling the conduit 13
At the same time, a part of it is introduced from the middle of the air heat exchanger 3 into the expansion tube 23, where it is cooled and introduced into the upper column of the rectification column 4. There is a method for cooling the feed air by introducing liquefied natural gas into the intercooler 25 of the air compressor 24 through the conduit 26, but the former method is effective when collecting gaseous oxygen and gaseous nitrogen. Moreover, in the latter method, there is a problem in that moisture and carbon dioxide gas in the feed air freeze in the intercooler 25.
本発明は、ガス酸素およびガス窒素を採取する空気分離
装置において、上述の問題を解決すると共に動力消費量
を減少することを目的としたものである。本発明は、約
１に９／ｃｌｔＧに圧縮した原料空気を脱湿し、空気熱
交換器で飽和温度まで冷却して精留塔に導入し、精留塔
で分離した窒素ガスの一部、を窒素熱交換器を通して約
−１６５℃まで温度回復させた後窒素圧縮機で約５に９
／ａｉＧに圧縮し、圧縮により温度上昇した窒素ガスを
液化天然ガスの寒冷で約−１５０℃に冷却した後、前記
窒素熱交換器を通して飽和温度まて冷却し、精留塔内の
液体丁酸素と熱交換させて液化した後約１に９／ｄＧに
減圧して精留塔内に導入するようにしたものである。The present invention aims to solve the above-mentioned problems and reduce power consumption in an air separation device for collecting gaseous oxygen and gaseous nitrogen. The present invention dehumidifies raw air compressed to about 1 to 9/cltG, cools it to saturation temperature with an air heat exchanger, and introduces it into a rectification column, and a part of the nitrogen gas separated in the rectification column, After recovering the temperature to about -165℃ through a nitrogen heat exchanger, it was heated to about 5 to 9 degrees Celsius using a nitrogen compressor.
/aiG, and the nitrogen gas whose temperature has risen due to compression is cooled to approximately -150°C by liquefied natural gas cooling, and then cooled to the saturation temperature through the nitrogen heat exchanger, and the liquid nitrogen gas in the rectification column is cooled to a saturation temperature. After liquefying it by heat exchange with the liquid, the pressure is reduced to about 1 to 9/dG and the mixture is introduced into a rectification column.
以下、本発明を実施した装置の一例を第２図によつて説
明する。An example of an apparatus embodying the present invention will be described below with reference to FIG.
第２図において、１は原料空気のブロワ、２は原料空気
中の水分および炭酸ガスを吸着除去する脱湿塔で弁１１
により交互に切替えて使用される。３は原料空気と低温
戻りガスとを熱交換させて原料空気を飽和温度まで冷却
すると同時に低温戻りガスを常温まで温度回復させる空
気熱交換器４は原料空気を深冷分離する精留塔５は窒素
熱交換器、６は窒素圧縮機、７は液化天然ガス用の熱交
換器、８は精留塔４内下部に設けられた凝縮器であつて
、原料空気をブロワ１で約１ｋｇ／Ｃ７ｌｆＧに圧縮し
、脱湿塔２で水分および炭酸ガスを吸着除去する。In Fig. 2, 1 is a feed air blower, 2 is a dehumidification tower that adsorbs and removes moisture and carbon dioxide from the feed air, and valve 11 is shown.
It is used by switching alternately. 3 is an air heat exchanger 4 that exchanges heat between the feed air and the low-temperature return gas to cool the feed air to the saturation temperature and at the same time recovers the temperature of the low-temperature return gas to room temperature; and the rectifier 5 that cryogenically separates the feed air. A nitrogen heat exchanger, 6 a nitrogen compressor, 7 a heat exchanger for liquefied natural gas, and 8 a condenser installed in the lower part of the rectification column 4. The dehumidifying tower 2 adsorbs and removes moisture and carbon dioxide.
脱湿された原料空気は、空気熱交換器３で導管１０，１
４，２２よりの低温戻りガスと熱交換して飽和温度まで
冷却された後、導管１３より精留塔４に導入される。精
留塔４で精留分離された高純度窒素ガスの一部は、導管
１４より空気熱交換器３に導入され、原料空気を冷却し
て温度回復した後製品窒素ガスとして取出される。The dehumidified raw air is passed through the air heat exchanger 3 to conduits 10 and 1.
After being cooled to saturation temperature by exchanging heat with the low-temperature return gas from 4 and 22, it is introduced into the rectification column 4 through a conduit 13. A part of the high-purity nitrogen gas that has been rectified and separated in the rectification column 4 is introduced into the air heat exchanger 3 through a conduit 14, and after cooling the raw air and recovering the temperature, it is taken out as a product nitrogen gas.
また、一部の高純度窒素ガスは、窒素熱交換器５を通し
て約−１６５℃まで温度回復された後、導管１５より窒
素圧縮機６に導入され、窒素圧縮機６で約５ｋ９／Ｃｒ
ｌＧに圧縮される。この圧縮により温度上昇した窒素ガ
スは熱交換器７に導入され、導管１６より熱交換器７に
入り窒素ガスと熱交換して蒸発し導管１７より出て行く
約−１６０℃の液化天然ガスにより、約−１５０℃に冷
却された後導管１８より窒素熱交換器５に導入され、更
に約−１７８℃まで冷却されて導管１９，より精留塔４
の内下部の凝縮器８へ導入される。凝縮器８内に導入さ
れた窒素ガスは、精留塔４内下部に精留分離された液体
酸素と熱交換して液体窒素となり、導管２０を通つて弁
１２で精留塔４内圧力まで減圧された後、導管２１より
精留塔４二内に環流液として導入される。一方、窒素ガ
スと熱交換してガス化された酸素ガスの一部は、導管２
２より空気熱交換器３に導入され、原料空気を冷却して
常温まで温度回復した後製品酸素ガスとして取出され、
残りの酸素ガスは上昇ガスとして４精留塔４内を上昇す
る。また、精留塔４内のパージガスは、導管１０より空
気熱交換器３に導入され、原料空気を冷却して常温まで
温度回復した後大気に放出される。上述の実施例では、
液化天然ガス用の熱交換器７を窒素圧縮機６のアフター
クーラとして使用したものについて説明したが、熱交換
器７を窒素圧縮機６のインタ−クーラー９として使用す
ることもできる。In addition, some high-purity nitrogen gas is recovered to a temperature of about -165°C through the nitrogen heat exchanger 5, and then introduced into the nitrogen compressor 6 through the conduit 15, where it is heated to about 5k9/Cr.
It is compressed to 1G. The nitrogen gas, whose temperature has increased due to this compression, is introduced into the heat exchanger 7 through the conduit 16, exchanges heat with the nitrogen gas, evaporates, and exits through the conduit 17 with liquefied natural gas at approximately -160°C. After being cooled to about -150°C, it is introduced into the nitrogen heat exchanger 5 through conduit 18, further cooled to about -178°C, and then passed through conduit 19 to rectification column 4.
is introduced into the condenser 8 in the inner lower part of the . The nitrogen gas introduced into the condenser 8 exchanges heat with the liquid oxygen that has been rectified and separated in the lower part of the rectification column 4 to become liquid nitrogen, and passes through the conduit 20 and reaches the internal pressure of the rectification column 4 at the valve 12. After the pressure is reduced, it is introduced into the rectification column 42 through the conduit 21 as a reflux liquid. On the other hand, a part of the oxygen gas gasified by heat exchange with nitrogen gas is transferred to the conduit 2.
2 is introduced into the air heat exchanger 3, and after cooling the raw air and recovering the temperature to room temperature, it is taken out as a product oxygen gas.
The remaining oxygen gas rises in the four rectification towers 4 as rising gas. Further, the purge gas in the rectification column 4 is introduced into the air heat exchanger 3 through the conduit 10, cools the raw air, and after recovering the temperature to room temperature, is released into the atmosphere. In the example described above,
Although the heat exchanger 7 for liquefied natural gas has been described as an aftercooler for the nitrogen compressor 6, the heat exchanger 7 can also be used as an intercooler 9 for the nitrogen compressor 6.
本発明は以上述べたように、窒素熱交換器を出た約−１
６５℃の窒素ガスを、窒素圧縮機でほぼ大気圧から約５
ｋｇ／Ｃ７ｌｆＧに圧縮するようにしたものであつて、
圧縮機の理論動力は吸入ガスの絶対温度に比例するので
、大気温度の原料空気を圧縮する従来の原料空気圧縮機
に比べて消費動力を著しく低減することができると共に
、窒素圧縮機における処理風量も原料空気量より少なく
、圧縮機容量も原料空気圧縮機に比べて小型化すること
がで７き、消費動力を更に減少することができる。As described above, the present invention provides approximately -1
Nitrogen gas at 65°C is reduced from atmospheric pressure to approximately 5°C using a nitrogen compressor.
kg/C7lfG,
The theoretical power of the compressor is proportional to the absolute temperature of the intake gas, so the power consumption can be significantly reduced compared to conventional raw material air compressors that compress raw material air at ambient temperature, and the processing air volume in the nitrogen compressor can be reduced significantly. The compressor capacity is also smaller than that of the raw air compressor, and the power consumption can be further reduced.
また、約５ｋ９／Ｃ７ｌｉＧの窒素ガスを液化天然ガス
の寒冷を利用して冷却するようにしたものであるから、
安全性が高く、熱交換器の設計、製作が容易である。更
に、寒冷発生源としての膨脹タビーンを必要としないた
め、従来装置で膨脹のために使用されていた約５ｋｇ／
ＡｉＧ原料空気が不要となり、原料空気量を減少するこ
とができる。In addition, since the nitrogen gas of approximately 5k9/C7liG is cooled using the cold of liquefied natural gas,
It is highly safe and the heat exchanger is easy to design and manufacture. Furthermore, since there is no need for an expansion tabine as a source of cold generation, the approximately 5 kg/kg amount used for expansion in conventional equipment can be reduced.
AiG raw material air is no longer necessary, and the amount of raw material air can be reduced.
更にまた、精留塔には約１ｋ９／ＣｌｔＧの原料空気を
導入するようにしたものであるから、従来の約５ｋｇ／
ＣＩｔＧの原料空気を導入する精留塔に比べて塔内圧力
が低圧となり、安全性の向上ならびに材料費を低減する
ことができると共に、塔内圧力が同一であるため１塔式
とすることができ、従来の窒素圧縮機または空気圧縮機
を使用した中圧回路を有する空気分離装置に比べて、装
置全体が簡単になり、構成機器も少なく、設備価格を低
減することができると同時に運転、保守が容易になり、
従来の方法に比べて安価なガス酸素およびガス窒素を採
取することができる。Furthermore, since feed air of about 1k9/CltG is introduced into the rectification column, the amount of feed air introduced into the rectification column is reduced from about 5kg/CltG to the conventional method.
Compared to the rectification column that introduces raw air for CItG, the pressure inside the column is lower, improving safety and reducing material costs, and since the pressure inside the column is the same, it is possible to use a single column type. Compared to an air separation device with a medium pressure circuit using a conventional nitrogen compressor or air compressor, the entire device is simpler and has fewer components, reducing equipment costs, and at the same time is easy to operate and operate. Maintenance becomes easier;
Gaseous oxygen and gaseous nitrogen can be extracted at a lower cost than conventional methods.
第１図は従来の空気熱分離装置の一例を示す系統図、第
２図は本発明を実施した空気熱分離装置の一例を示す系
統図である。
１・・・・・・ブロワ、２・・・・・・脱湿塔、３・・
・・・・空気熱交換器、４・・・・・・精留塔、５・・
・・・・窒素熱交換器、６・・・・・・窒素圧縮機、７
・・・・・・液化天然ガス用の熱交換器、８・・・・・
・凝縮器、９，２５・・・・・・インタ−クーラー、１
１，１２・・・・・・弁、１０，１３〜２２，２６・・
・導管、２３・・・・・・膨脹タービン、２４・・・・
・・原料空気圧縮機。FIG. 1 is a system diagram showing an example of a conventional air-thermal separation device, and FIG. 2 is a system diagram showing an example of an air-thermal separation device in which the present invention is implemented. 1...Blower, 2...Dehumidification tower, 3...
... Air heat exchanger, 4 ... Rectification column, 5 ...
...Nitrogen heat exchanger, 6...Nitrogen compressor, 7
...Heat exchanger for liquefied natural gas, 8...
・Condenser, 9, 25...Intercooler, 1
1, 12... Valve, 10, 13-22, 26...
- Conduit, 23... Expansion turbine, 24...
... Raw material air compressor.
Claims (1)
気を空気熱交換器で低温戻りガスと熱交換させて冷却し
た後精留塔に導入して深冷分離する空気分離装置におい
て、約１ｋｇ／ｃｍ＾２Ｇに圧縮した原料空気を脱湿塔
で脱湿し、空気熱交換器で低温戻りガスと熱交換させて
飽和温度まで冷却した後精留塔に導入し、精留塔で分離
された窒素ガスの一部を窒素熱交換器を通して約−１６
５℃まで温度回復させた後窒素圧縮機で約５ｋｇ／ｃｍ
＾２Ｇに圧縮し、熱交換器で液化天然ガスと熱交換させ
た約−１５０℃に冷却した後、前記窒素熱交換器を通し
て飽和温度まで冷却して精留塔下部に導入し、液体酸素
と熱交換させて液化した後約１ｋｇ／ｃｍ＾２Ｇに減圧
して精留塔内に環流液として導入するようにしたことを
特徴とする液化天然ガスの寒冷を利用した空気分離方法
。1 In an air separation device that removes water and carbon dioxide gas by adsorption in a dehumidification tower, the raw air is cooled by exchanging heat with low-temperature return gas in an air heat exchanger, and then introduced into a rectification tower for cryogenic separation.Approximately 1 kg The raw air compressed to /cm^2G is dehumidified in a dehumidification tower, cooled to saturation temperature by exchanging heat with low-temperature return gas in an air heat exchanger, and then introduced into a rectification tower where it is separated. A portion of the nitrogen gas is passed through a nitrogen heat exchanger to approximately -16
After recovering the temperature to 5℃, use a nitrogen compressor to reduce the pressure to about 5kg/cm.
It is compressed to 2G, cooled to approximately -150°C by heat exchange with liquefied natural gas in a heat exchanger, cooled to saturation temperature through the nitrogen heat exchanger, and introduced into the lower part of the rectification column, where it is mixed with liquid oxygen. An air separation method using refrigeration of liquefied natural gas, characterized in that the liquefied natural gas is liquefied by heat exchange and then depressurized to about 1 kg/cm^2G and introduced into a rectification column as a reflux liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3853377A JPS6044583B2 (en) | 1977-04-06 | 1977-04-06 | Air separation method using cooling of liquefied natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3853377A JPS6044583B2 (en) | 1977-04-06 | 1977-04-06 | Air separation method using cooling of liquefied natural gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS53124169A JPS53124169A (en) | 1978-10-30 |
| JPS6044583B2 true JPS6044583B2 (en) | 1985-10-04 |
Family
ID=12527906
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3853377A Expired JPS6044583B2 (en) | 1977-04-06 | 1977-04-06 | Air separation method using cooling of liquefied natural gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6044583B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0814458B2 (en) * | 1987-07-10 | 1996-02-14 | 日本酸素株式会社 | Nitrogen production method |
| CN105783424B (en) * | 2016-04-22 | 2017-12-12 | 暨南大学 | The air separating method of high-pressure oxygen-enriched gas is produced using cold energy of liquefied natural gas |
-
1977
- 1977-04-06 JP JP3853377A patent/JPS6044583B2/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS53124169A (en) | 1978-10-30 |
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