JPS6155027B2 - - Google Patents
Info
- Publication number
- JPS6155027B2 JPS6155027B2 JP53072148A JP7214878A JPS6155027B2 JP S6155027 B2 JPS6155027 B2 JP S6155027B2 JP 53072148 A JP53072148 A JP 53072148A JP 7214878 A JP7214878 A JP 7214878A JP S6155027 B2 JPS6155027 B2 JP S6155027B2
- Authority
- JP
- Japan
- Prior art keywords
- sub
- rectification column
- oxygen
- condenser
- nitrogen
- 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
- F25J3/04248—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
-
- 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
- F25J3/04436—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 at least a triple pressure main column system
- F25J3/04454—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 at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
-
- 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
- F25J2200/30—Processes or apparatus using separation by rectification using a side column in a single pressure column system
-
- 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
- F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
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、窒素製造装置において少量の酸素を
製造する方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for producing small amounts of oxygen in a nitrogen production apparatus.
近年、シールおよびパージ用あるいは化学反応
用として中、小容量の窒素製造装置の需要が高ま
つている。本発明は、その窒素製造装置におい
て、窒素製造量に比べ小量ではあるが酸素を製造
する必要がある場合に適するもので、従来の窒素
製造装置に付設することにより酸素を製造するも
のである。一般に知られている窒素製造装置は、
簡単な構成で操作性が良く、製品窒素は直接装置
から圧力下で採取できる等の利点を持つている
が、この窒素製造装置のもつ利点をそのまま生か
し、さらに少量の酸素が採取できるということ
が、従来の深冷分離による窒素および酸素製造装
置と本発明の大きな相違点である。 In recent years, there has been an increasing demand for medium to small capacity nitrogen production equipment for sealing and purging purposes or for chemical reactions. The present invention is suitable for cases where the nitrogen production equipment needs to produce oxygen, albeit in a small amount compared to the amount of nitrogen produced, and can be attached to a conventional nitrogen production equipment to produce oxygen. . Generally known nitrogen production equipment is
It has a simple configuration and good operability, and has the advantage of being able to collect product nitrogen directly from the device under pressure.However, it is possible to take advantage of the advantages of this nitrogen production device and collect even smaller amounts of oxygen. This is a major difference between the present invention and conventional nitrogen and oxygen production equipment using cryogenic separation.
第１図は従来の窒素製造装置の一例を示し、吸
着塔により原料空気中の水分を除去しガス窒素の
みを採取する場合の概略系統図である。図におい
て、原料空気は原料空気圧縮機１により所定の圧
力に昇圧され、吸着塔２へ導かれて水分および炭
酸ガスが吸着除去される。なお、原料空気圧縮機
１と吸着塔２の間に冷却器等を設け、吸着塔能力
をあげる場合も多い。吸着塔２を出た原料空気は
熱交換器３により冷却され、一部液化した状態で
精留塔４に入り精留される。精留された窒素は精
留塔４の上部より取り出され、熱交換器３を通つ
て温度回復した後需要先へ供給される。一方、精
留塔４の底部に溜る酸素分に富んだ液体空気は凝
縮器５に送られて凝縮器５によつてガス化され、
膨張タービン６により寒冷を発生させた後、熱交
換器３で原料空気と熱交換し温度回復して外気に
放出される。 FIG. 1 shows an example of a conventional nitrogen production apparatus, and is a schematic system diagram in which moisture is removed from raw air using an adsorption tower and only gaseous nitrogen is collected. In the figure, raw air is pressurized to a predetermined pressure by a raw air compressor 1, and is led to an adsorption tower 2 where water and carbon dioxide are adsorbed and removed. Note that in many cases, a cooler or the like is provided between the raw air compressor 1 and the adsorption tower 2 to increase the adsorption tower capacity. The raw air leaving the adsorption tower 2 is cooled by a heat exchanger 3, and enters a rectification tower 4 in a partially liquefied state to be rectified. The rectified nitrogen is taken out from the upper part of the rectification column 4, passed through a heat exchanger 3, and after its temperature is recovered, it is supplied to a consumer. On the other hand, the oxygen-rich liquid air accumulated at the bottom of the rectification column 4 is sent to the condenser 5 and gasified by the condenser 5.
After the expansion turbine 6 generates cold, the heat exchanger 3 exchanges heat with the raw material air to recover the temperature and discharge it to the outside air.
第２図は副精留塔を従来の窒素製造装置に付設
し、製品窒素は従来と同様に採取し、加えて酸素
を採取できるようにした本発明方法の概略系統図
である。この第２図においても窒素製造装置は第
１図で説明したように運転される。凝縮器５に溜
る液体空気の一部は導管９を介して付設された副
精留塔８へ導かれ、副精留塔８の下降液となる。
一方、原料空気の一部は精留塔４に入る前から導
管１０により副精留塔８に内蔵された副凝縮器７
に導かれ、副精留塔８底部に溜る液体酸素と熱交
換し、副精留塔８の上昇ガスを作る。副精留塔８
で酸素に富んだ液体空気から精留分離された酸素
は、導管１２により副精留塔８から取り出され、
製品窒素と同様に熱交換器３で常温まで温度回復
した後需要先へ供給される。一方、残りの廃ガス
は副精留塔８の頂部より導管１３によつて取り出
され、窒素製造装置の廃ガスラインに戻されて放
出される。なお、酸素はガス状で採取できるのみ
でなく、導管１４から液状としても採取できる。 FIG. 2 is a schematic system diagram of the method of the present invention in which a sub-rectification column is attached to a conventional nitrogen production apparatus, product nitrogen is collected in the same manner as before, and oxygen can also be collected in addition. Also in FIG. 2, the nitrogen production apparatus is operated as explained in FIG. A part of the liquid air accumulated in the condenser 5 is led to an attached sub-rectification column 8 via a conduit 9, and becomes a descending liquid of the sub-rectification column 8.
On the other hand, before entering the rectifying column 4, a part of the raw air is passed through a conduit 10 to a sub-condenser 7 built in the sub-rectifying column 8.
The gas exchanges heat with the liquid oxygen accumulated at the bottom of the sub-rectification column 8 to produce rising gas in the sub-rectification column 8. Sub-rectification column 8
The oxygen separated by rectification from the oxygen-rich liquid air is taken out from the sub-rectification column 8 through a conduit 12,
Like the product nitrogen, the temperature is recovered to room temperature in the heat exchanger 3 before being supplied to the consumer. On the other hand, the remaining waste gas is taken out from the top of the sub-rectification column 8 through a conduit 13, returned to the waste gas line of the nitrogen production device, and discharged. Note that oxygen can be collected not only in gaseous form but also in liquid form from the conduit 14.
なお、本発明は吸着塔を使用した場合に限らず
可逆熱交換器方式の場合にも、さらにガス状窒素
のみ採取する場合および液体窒素も併せ採取する
場合にも適用できる。 Note that the present invention is applicable not only to the case where an adsorption tower is used, but also to the case of a reversible heat exchanger system, and also to the case where only gaseous nitrogen is collected and the case where liquid nitrogen is also collected.
以上述べた如く、本発明によれば窒素製造装置
の特徴を生かしてさらに少量の酸素および液体酸
素を採取できる効果がある。 As described above, according to the present invention, it is possible to take advantage of the features of the nitrogen production apparatus to collect even smaller amounts of oxygen and liquid oxygen.
第１図は従来より使用されているガス窒素採取
の窒素製造装置の概略系統図、第２図は本発明方
法を示す概略系統図である。
１……原料空気圧縮機、２……吸着塔、３……
熱交換器、４……精留塔、５……凝縮器、６……
膨張タービン、７……副凝縮器、８……副精留
塔。
FIG. 1 is a schematic system diagram of a conventionally used nitrogen production apparatus for gaseous nitrogen extraction, and FIG. 2 is a schematic system diagram showing the method of the present invention. 1... Raw material air compressor, 2... Adsorption tower, 3...
Heat exchanger, 4... Rectification column, 5... Condenser, 6...
Expansion turbine, 7... sub-condenser, 8... sub-rectification column.
Claims (1)
後冷却液化して精留塔で深冷分離する窒素製造装
置において、副凝縮器を内蔵した副精留塔の頂部
に前記精留塔凝縮器の液体空気の一部を導入し、
副凝縮器に精留塔に導入する原料空気の一部を導
入し副精留塔底部の液体酸素と熱交換させて上昇
ガスを発生させ、液化した原料空気を精留塔に戻
すと共に副精留塔底部より酸素を採取することを
特徴とする窒素製造装置における酸素採取法。1. In a nitrogen production device that removes moisture and carbon dioxide from feed air, cools it to liquefy, and then deep-cools and separates it in a rectification column, the rectification column condenser is installed at the top of the sub-rectification column that has a built-in sub-condenser. Introducing a portion of liquid air,
A part of the feed air to be introduced into the rectification column is introduced into the sub-condenser, where it exchanges heat with the liquid oxygen at the bottom of the sub-condenser to generate rising gas. An oxygen collection method for a nitrogen production device, which is characterized by collecting oxygen from the bottom of a distillation column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7214878A JPS54163797A (en) | 1978-06-16 | 1978-06-16 | Oxygen sampling method in nitrogen producing apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7214878A JPS54163797A (en) | 1978-06-16 | 1978-06-16 | Oxygen sampling method in nitrogen producing apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS54163797A JPS54163797A (en) | 1979-12-26 |
| JPS6155027B2 true JPS6155027B2 (en) | 1986-11-26 |
Family
ID=13480882
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7214878A Granted JPS54163797A (en) | 1978-06-16 | 1978-06-16 | Oxygen sampling method in nitrogen producing apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS54163797A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6115066A (en) * | 1984-07-02 | 1986-01-23 | 大同酸素株式会社 | Production unit for high-purity nitrogen gas |
| JPS6115069A (en) * | 1984-07-02 | 1986-01-23 | 大同酸素株式会社 | Production unit for high-purity nitrogen gas |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5241232B2 (en) * | 1972-01-31 | 1977-10-17 | ||
| JPS5541855B2 (en) * | 1973-08-14 | 1980-10-27 | ||
| DE2542468A1 (en) * | 1975-09-24 | 1977-04-07 | Bayer Ag | HERBICIDAL AGENT |
-
1978
- 1978-06-16 JP JP7214878A patent/JPS54163797A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS54163797A (en) | 1979-12-26 |
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