JPH02293576A - air separation equipment - Google Patents
air separation equipmentInfo
- Publication number
- JPH02293576A JPH02293576A JP11371789A JP11371789A JPH02293576A JP H02293576 A JPH02293576 A JP H02293576A JP 11371789 A JP11371789 A JP 11371789A JP 11371789 A JP11371789 A JP 11371789A JP H02293576 A JPH02293576 A JP H02293576A
- Authority
- JP
- Japan
- Prior art keywords
- air
- column
- conduit
- rectification
- liquid
- 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
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
- F25J3/04406—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
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
- F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high pressure column of a double pressure main column system
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
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は膨張タービンおよび深冷分離装置を有する空気
分離装置に関するものである。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to an air separation device having an expansion turbine and a cryogenic separation device.
従来の深冷分離方法を用いた空気分離ｉｔにおいて、膨
張タービンで膨張された空気又は窒素は精管塔に吹込れ
ており、膨張された空気又は窓素が加熱状態であっても
同様であった。以下、第２図により詳細を説明する。In air separation IT using conventional cryogenic separation methods, air or nitrogen expanded by an expansion turbine is blown into a vasophage column, and the same is true even if the expanded air or window element is heated. Ta. Details will be explained below with reference to FIG.
図において、空気分離装置の前処理装置で水分および炭
酸ガスを除去された原料空気の大部分は導管１． ２
より空気熱交換器３に導入され、冷却後導管４を経て精
留塔下部塔６へ供給される。精留塔下部塔６の頂部に設
置される凝縮器諺で液体酸素によって凝縮された液体窓
素は精留分離にょって精留塔下部塔６の底部では液体空
気となって溜まる。この液体空気は導管７．８を経て熱
交換器９で過冷却された後，導管１０を経て膨張弁１１
で減圧され、導管認な経て精留塔上部塔ｌ３へ送入され
る。精留塔上部塔ｌから導管１４により抜出される廃窒
素は熱交換器９にて昇湿され、さらに導管１５により空
気熱交換器３に供給されて、常温まで温度回復して導管
ｌ６より送出される。In the figure, most of the raw air from which moisture and carbon dioxide have been removed in the pre-treatment device of the air separation device is piped into conduit 1. 2
It is then introduced into the air heat exchanger 3, and after being cooled, it is supplied to the lower column 6 of the rectification column via the conduit 4. In the condenser installed at the top of the lower column 6 of the rectification column, the liquid window element condensed by liquid oxygen is collected as liquid air at the bottom of the lower column 6 of the rectification column by rectification separation. This liquid air passes through a conduit 7.8, is supercooled in a heat exchanger 9, and then passes through a conduit 10 to an expansion valve 11.
The pressure is reduced at , and the product is sent to the upper column 13 of the rectification column via a conduit. The waste nitrogen extracted from the upper column 1 of the rectification column through the conduit 14 is humidified in the heat exchanger 9, and further supplied to the air heat exchanger 3 through the conduit 15, where the temperature is recovered to room temperature and sent out through the conduit 16. be done.
また導管１から導管１７へ分岐する原料空気の一部はタ
ービン圧縮ｉａ１ｇで昇圧された後、導管１９を経て後
方冷却器加で冷却され、導管４を経て空気熱交換器３へ
供給される。空気熱交換器３で所定の温度まで冷却され
た後、導管４を経てタービン圧縮ａ１８で膨張し、導管
５を経て精留塔上部塔ｌへ送入される。Further, a part of the feed air branched from the conduit 1 to the conduit 17 is pressurized by the turbine compression ia1g, passes through the conduit 19, is cooled by a back cooler, and is supplied to the air heat exchanger 3 via the conduit 4. After being cooled to a predetermined temperature in the air heat exchanger 3, it is expanded through the turbine compression a18 through the conduit 4, and is sent through the conduit 5 to the upper column 1 of the rectification column.
一方、精留塔下部塔６の頂部より導管囚で抜き出される
液体窒素は熱交換器９で過冷却された後、導管クを経て
膨張弁（９）で減圧され、導管３ｌを経て精ｇＩＩ塔上
部塔ｌ３の頂部へ送入される。On the other hand, the liquid nitrogen extracted from the top of the lower column 6 of the rectification column by a conduit is supercooled in a heat exchanger 9, passes through a conduit 6, is depressurized by an expansion valve (9), and passes through a conduit 3l to a fraction gII. It is fed into the top of the upper column 13.
さらにまた″精留塔上部塔口の底部に溜まった液体酸素
は凝縮器《において精留塔下部塔６の窒素ガスと熱交換
し、蒸発して酸素ガスとなり、一部導管《によって抜き
出される。導管羽によって抜き出された酸素ガスは空気
熱交換器３へ供給され、常温まで温度回復して導管翼よ
り送出される。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６２−１４２９８４号が挙げられる。Furthermore, the liquid oxygen accumulated at the bottom of the upper column mouth of the rectifying column exchanges heat with the nitrogen gas in the lower column 6 of the rectifying column in the condenser, evaporates into oxygen gas, and is partially extracted through the conduit. The oxygen gas extracted by the conduit vanes is supplied to the air heat exchanger 3, where the temperature is recovered to room temperature and sent out from the conduit vanes. -142984 is mentioned.
上記従来技術は酸素ガスの精留効率について配慮がされ
ておらず、タービン圧縮機を出た空気の温度が高い場合
でもそのまま精留塔へ送入され、精留塔上部塔の上部の
下降液を一部蒸発させ、精留塔上部塔の下部からの上昇
ガスと合流している。The above conventional technology does not take into account the rectification efficiency of oxygen gas, and even if the temperature of the air exiting the turbine compressor is high, it is directly sent to the rectification column, and the descending liquid at the top of the upper column of the rectification column is Part of the gas is evaporated and the gas is combined with the rising gas from the bottom of the upper column of the rectification column.
このため酸素ガスの精留効率を決める精留塔上部塔の下
部の環流流量がその分少な畷なり、精留効率が低下する
という欠点があった。For this reason, the recirculation flow rate at the lower part of the upper column of the rectification column, which determines the rectification efficiency of oxygen gas, is correspondingly small, resulting in a disadvantage that the rectification efficiency is lowered.
本発明の目的は上記酸素ガスの精留効率を改善する空気
分離装置を提供することにある。An object of the present invention is to provide an air separation device that improves the rectification efficiency of oxygen gas.
上記目的を達成するため、新たに熱交換器な設け、該熱
交換器によりタービン圧縮機を出た加熱空気と精留塔下
部塔の底部の液体空気とを熱交換させたものである。In order to achieve the above object, a heat exchanger is newly installed, and the heat exchanger exchanges heat between the heated air exiting the turbine compressor and the liquid air at the bottom of the lower column of the rectification column.
新たに設けた熱交換器において、タービン圧縮機を出た
加熱空気と熱交換して蒸発した液体空気の一部は、精留
塔下部塔の下部に供給される原料空気と共に上昇し、精
留塔下部塔の頂部に設置されている凝縮器において液体
酸素と熱交換する。In the newly installed heat exchanger, a part of the liquid air that evaporates by exchanging heat with the heated air exiting the turbine compressor rises together with the feed air supplied to the lower part of the lower column of the rectification column, and is used for rectification. Heat exchanges with liquid oxygen in the condenser installed at the top of the lower column column.
凝縮器で蒸発した酸素は上昇ガスとなり、精留塔上部塔
内を上昇する。Oxygen evaporated in the condenser becomes a rising gas and rises in the upper column of the rectification column.
従って精留塔下部塔および精留塔上部塔下部の上昇ガス
が、精留塔下部塔底部で発生した蒸発した分だけ増加す
ることになる。Therefore, the rising gas in the lower column of the rectification column and the lower part of the upper column of the rectification column increases by the amount of evaporation generated at the bottom of the lower column of the rectification column.
即ち精留塔内において環流流量が増加し、精留効率が改
善される。That is, the reflux flow rate increases in the rectification column, and the rectification efficiency is improved.
以下、本発明の一実施例をＷｉｌ図により説明する。 An embodiment of the present invention will be described below using Wil diagrams.
図において、空気分離装置の前処理装置で水分および炭
酸ガスを除去された原料空気の大部分は導管１．２より
空気熱交換器３に導入され、冷却後導管４を経て精留塔
下部埼６へ供給される。精留塔下部塔６の頂部に設置さ
れる凝縮器冨で液体酸素によって凝縮された液体窒素は
精留分離によって精留培下部塔６の底部では液体空気と
なって溜まる。この液体空気の大部分は導管７，８を経
て熱交換器９で過冷却された後、導管１０を経て膨張弁
Ｕで減圧され、導管校を経て精留塔上部塔１３へ送入さ
れる。また、液体空気の一部は導管７，々を経て熱交換
器冴においてタービン出口空気によって加熱蒸発され、
導管ｎを経て精留塔下部塔６へ戻る。In the figure, most of the raw air from which moisture and carbon dioxide have been removed in the pretreatment device of the air separation device is introduced into the air heat exchanger 3 through conduit 1.2, and after being cooled, it passes through conduit 4 to the lower part of the rectification column. 6. Liquid nitrogen condensed by liquid oxygen in a condenser installed at the top of the lower column 6 of the rectification column becomes liquid air and accumulates at the bottom of the lower column 6 of the rectification medium by rectification separation. Most of this liquid air passes through conduits 7 and 8, is supercooled in a heat exchanger 9, passes through a conduit 10, is depressurized by an expansion valve U, and is sent to the upper column 13 of the rectification column via a conduit. . Also, a part of the liquid air is heated and evaporated by the turbine outlet air in the heat exchanger through the conduits 7, etc.
It returns to the lower column 6 of the rectification column via conduit n.
精留塔下部塔６の頂部より導管怨で抜き出される液体窒
素は熱交換器９で過冷゜却された後、導管四を経て膨張
弁（資）で減圧され、導管阻を経て精留塔下部塔口の頂
部へ送入される。The liquid nitrogen extracted from the top of the lower column 6 of the rectifying column through a conduit is subcooled in a heat exchanger 9, passes through conduit 4, is depressurized by an expansion valve, and is then rectified through a conduit. It is sent to the top of the tower mouth at the bottom of the tower.
また、導管ｌから導管ｌ７へ分岐する原料空気の一部は
タービン圧縮機厚８で昇圧された後、導管ｌ９を経て後
方冷却器囚で冷却され、導管４を経て空気熱交換器３へ
供給される。空気熱交換器３で所定の温度まで冷却され
た後、導管ｎを経てタービン圧縮機１８で膨張した後、
導管器を経て熱交換器スヘ供給される。熱交換器スにお
いて精留塔下部塔６の液体空気の一部と熱交換して冷却
された後、導管２を経て精留塔上部塔口へ送入される。In addition, a part of the raw material air branched from the conduit l to the conduit l7 is pressurized by the turbine compressor thickness 8, is cooled in the rear cooler via the conduit l9, and is supplied to the air heat exchanger 3 via the conduit 4. be done. After being cooled to a predetermined temperature in the air heat exchanger 3, it is expanded in the turbine compressor 18 through the conduit n, and then
It is supplied to the heat exchanger via a conduit. After being cooled by heat exchange with a part of the liquid air in the lower column 6 of the rectification column in the heat exchanger, it is sent to the upper column mouth of the rectification column through the conduit 2.
精留塔上部塔１３の底部に溜った液体酸素は凝縮器《に
おいて精留塔下部塔６の窒素ガスと熱交換し、蒸発して
酸素ガスとなり、一部導管おによって抜き出される。導
管冨によって抜き出された酸素ガスは空気熱交換器３へ
供給され、常温まで温度回復して導管あより送出される
。The liquid oxygen accumulated at the bottom of the upper column 13 of the rectification column exchanges heat with the nitrogen gas in the lower column 6 of the rectification column in the condenser, evaporates into oxygen gas, and is partially extracted through a conduit. The oxygen gas extracted through the conduit is supplied to the air heat exchanger 3, the temperature is recovered to room temperature, and the oxygen gas is sent out through the conduit.
一方精留塔上部塔１３から導管１４により抜き出される
廃窒素は熱交換器９Ｉこて昇温され、さらに導管正によ
り空気熱交換器３に供給されて、常温まで温度回復して
導管ｌ６より送出される。On the other hand, the waste nitrogen extracted from the upper column 13 of the rectification column through the conduit 14 is heated through the heat exchanger 9I, and is further supplied to the air heat exchanger 3 through the conduit main, where the temperature is recovered to room temperature and then passed through the conduit 16. Sent out.
以上の構成において、新たに設けた熱交換器Ｕにより、
タービン圧縮機１８を出た加熱空気と精留塔下部塔６の
底部の液体空気とを熱交換させることで、酸素ガスの精
留効率の改善を図るものである。In the above configuration, the newly installed heat exchanger U allows
By exchanging heat between the heated air exiting the turbine compressor 18 and the liquid air at the bottom of the lower column 6 of the rectifying column, the efficiency of rectifying oxygen gas is improved.
本実施例によれば下記の効果がある。According to this embodiment, the following effects are achieved.
（１） タービンの流量を原料空気流量のｔＯｔｓ，
タービン出口温度を−１３０℃、液体空気の温度を−１
７３℃とし、タービン出口空気を−１７１℃まで冷却す
ると、１３ｋｃａｌ／Ｎ７ＦＬ”の熱交換量となる。液
体空気の蒸発潜熱を５ ７ ｋｃａ １ ／Ｎ ｍ”と
すると１０ＸＩ３／５７＝２．３％精留塔の流量が増加
する。即ち原料空気流量が２．３％低減できる。(1) The turbine flow rate is the feed air flow rate tOts,
Turbine outlet temperature is -130℃, liquid air temperature is -1
If the temperature is 73°C and the turbine outlet air is cooled to -171°C, the heat exchange amount will be 13 kcal/N7FL". If the latent heat of vaporization of liquid air is 5 7 kca 1 /N m", 10XI3/57 = 2.3%. The flow rate of the rectification column increases. That is, the raw material air flow rate can be reduced by 2.3%.
（２） また上！ｅｔｉｔ項により原料空気圧縮機と
原料空気前処理装置の清費電力代が低減できる。また追
設する熱交換器の設備費が増加するが、原料空気圧縮機
と原料空気前処理装置の設備費が減少するので、全体と
しては設備費が低減できる。(2) Up again! The etit term allows the cost of electricity for the raw air compressor and the raw air pre-treatment device to be reduced. Furthermore, although the equipment cost of the additionally installed heat exchanger increases, the equipment cost of the raw air compressor and the raw air pretreatment device decreases, so the equipment cost can be reduced as a whole.
（３）精留塔下部塔において空気吹込部と底部との間に
精留部を設けた場合、精留塔下部塔頂部から窒素を採取
する空気分離装置においては、窓素中のアルゴン濃度な
精留部を設けない場合に比べ大巾に低減できる。(3) When a rectifying section is provided between the air blowing section and the bottom in the lower column of the rectifying column, in an air separation device that collects nitrogen from the top of the lower column of the rectifying column, the argon concentration in the window element This can be significantly reduced compared to the case without a rectification section.
本発明によれば、タービン圧縮機を出た加熱空気と精留
壜下部塔の底部の液体空気とを熱交換させ、熱交換後の
冷却された加熱空気な精留塔上部塔へ、また加熱蒸発さ
れた液体空気は精留塔下部塔へ、それぞれ戻すことによ
り、酸素ガスの精留効亭の改善を図ることができる。According to the present invention, the heated air exiting the turbine compressor and the liquid air at the bottom of the lower column of the rectifying bottle are subjected to heat exchange, and the cooled heated air after the heat exchange is transferred to the upper column of the rectifying column for heating. By returning the evaporated liquid air to the lower column of the rectifying column, it is possible to improve the efficiency of rectifying oxygen gas.
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。
６・・・・・・精留塔下部塔、７．２６・・・・・・液
体空気導管、１８・・・・・・タービン圧縮機、Ｚ３，
２５． ２７・・曲空気導管、オｌ圀FIG. 1 is a system diagram of an air separation device according to an embodiment of the present invention.
The figure is a system diagram of a conventional air separation device. 6... Lower column of rectification column, 7.26... Liquid air conduit, 18... Turbine compressor, Z3,
25. 27...Curved air conduit, origami
Claims (1)
膨張された原料空気と精留塔下部塔底部の液体空気とを
熱交換させるように構成したことを特徴とする空気分離
装置。 ２、請求項第１項記載の空気分離装置の精留塔下部塔に
おいて、空気吸込部と底部との間に精留部を設けたこと
を特徴とする空気分離装置。 ３、深冷分離による空気分離装置において、タービンで
膨張された原料空気と精留分離された液体空気とを熱交
換させる熱交換器を精留塔下部塔に内蔵したことを特徴
とする空気分離装置。 ４、請求項第１項、又は請求項第３項に記載の空気分離
装置の運転方法において、タービン出口の原料空気と精
留塔下部塔底部の液体空気とを熱交換させて原料空気を
低減させることを特徴とする空気分離装置の運転方法。 ５、深冷分離による空気分離方法において、タービンで
膨張された原料空気と精留塔下部塔底部の液体空気とを
熱交換させ、酸素の採取量を増加させることを特徴とす
る空気分離方法。[Scope of Claims] 1. An air separation device using cryogenic separation, characterized in that the air separation device is configured to exchange heat between raw air expanded by a turbine and liquid air at the bottom of a lower part of a rectification column. Device. 2. An air separation device according to claim 1, characterized in that in the lower column of the rectification column, a rectification section is provided between the air suction section and the bottom section. 3. An air separation device using cryogenic separation, characterized in that a heat exchanger for exchanging heat between raw air expanded by a turbine and liquid air separated by rectification is built into the lower column of the rectification column. Device. 4. In the method of operating an air separation device according to claim 1 or 3, the amount of feed air is reduced by heat exchange between the feed air at the turbine outlet and the liquid air at the bottom of the lower part of the rectification column. A method of operating an air separation device characterized by: 5. An air separation method using cryogenic separation, which is characterized by increasing the amount of oxygen collected by exchanging heat between raw air expanded in a turbine and liquid air at the bottom of the lower part of a rectification column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11371789A JPH02293576A (en) | 1989-05-08 | 1989-05-08 | air separation equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11371789A JPH02293576A (en) | 1989-05-08 | 1989-05-08 | air separation equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH02293576A true JPH02293576A (en) | 1990-12-04 |
Family
ID=14619359
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11371789A Pending JPH02293576A (en) | 1989-05-08 | 1989-05-08 | air separation equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH02293576A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07159026A (en) * | 1993-09-23 | 1995-06-20 | Air Prod And Chem Inc | Method for low temperature distillation of air for producinggas and/or liquid product form oxygen and nitrogen simultaneously |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5620980A (en) * | 1979-07-20 | 1981-02-27 | Air Liquide | Low temperature air separation method of and apparatus for production of high pressure oxygen |
| JPS581350A (en) * | 1981-06-26 | 1983-01-06 | Pioneer Electronic Corp | Fm stereophonic demodulator |
| JPS62162876A (en) * | 1985-10-04 | 1987-07-18 | ザ・ビ−オ−シ−・グル−プ・ピ−エルシ− | Gas-liquid catalytic method and device |
| JPH054691A (en) * | 1991-06-20 | 1993-01-14 | Tokico Ltd | Unloading system of tank trailer |
-
1989
- 1989-05-08 JP JP11371789A patent/JPH02293576A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5620980A (en) * | 1979-07-20 | 1981-02-27 | Air Liquide | Low temperature air separation method of and apparatus for production of high pressure oxygen |
| JPS581350A (en) * | 1981-06-26 | 1983-01-06 | Pioneer Electronic Corp | Fm stereophonic demodulator |
| JPS62162876A (en) * | 1985-10-04 | 1987-07-18 | ザ・ビ−オ−シ−・グル−プ・ピ−エルシ− | Gas-liquid catalytic method and device |
| JPH054691A (en) * | 1991-06-20 | 1993-01-14 | Tokico Ltd | Unloading system of tank trailer |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07159026A (en) * | 1993-09-23 | 1995-06-20 | Air Prod And Chem Inc | Method for low temperature distillation of air for producinggas and/or liquid product form oxygen and nitrogen simultaneously |
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