JPS648269B2 - - Google Patents
Info
- Publication number
- JPS648269B2 JPS648269B2 JP16894579A JP16894579A JPS648269B2 JP S648269 B2 JPS648269 B2 JP S648269B2 JP 16894579 A JP16894579 A JP 16894579A JP 16894579 A JP16894579 A JP 16894579A JP S648269 B2 JPS648269 B2 JP S648269B2
- Authority
- JP
- Japan
- Prior art keywords
- air
- pipe
- expanded
- expansion
- valve
- 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
- 238000000034 method Methods 0.000 claims description 11
- 238000005057 refrigeration Methods 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 230000000694 effects Effects 0.000 claims description 4
- 230000001172 regenerating effect Effects 0.000 description 12
- 238000001816 cooling Methods 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000009931 harmful effect Effects 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
- Jet Pumps And Other Pumps (AREA)
Description
【発明の詳細な説明】
本発明は空気を液化精溜して酸素と窒素に分離
する空気分離装置の起動法に関するもので、装置
起動時において無駄に消費されていた圧力エネル
ギーの有効利用によつて寒冷発生量の増加を図り
装置起動時間の短縮を可能としたものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for starting an air separation device that liquefies and rectifies air and separates it into oxygen and nitrogen. This makes it possible to increase the amount of cold generated and shorten the device start-up time.
例えば、再生式熱交換器を使用しかつ寒冷発生
を膨脹機によつて行う全低圧式の空気分離装置の
起動法は、約５Kg／cm2に圧縮した原料空気を再生
式熱交換器に通した後膨脹機にて断熱膨脹せしめ
寒冷を発生して前記再生式熱交換器に戻して該器
を冷却する。再生式熱交換器がある程度冷却され
ると、発生寒冷および原料空気の一部が精溜塔過
冷器あるいは液化器等に導入され、これ等を冷却
する等の操作によつて装置全体の冷却を行い精溜
塔内に導入された原料空気が液化され、精溜分離
に必要な条件が満足されて定常運転操作に入るの
が普通である。このような起動法において、通常
は起動時のみ使用される膨脹機が設けられて寒冷
発生量の増加を図つているが、原料空気量に対す
る膨脹機の処理能力が少ないため原料空気の余剰
分は圧縮後自由膨脹して大気に放出されていた。
これは圧縮動力が全く利用されず無駄であるばか
りか、大気に自由膨脹する際発する騒音による弊
害をもたらし、このための対策も必要とされてい
た。このようなことから圧縮原料空気の余剰分を
大気へ自由膨脹せず装置内で自由膨脹せしめ、得
られた寒冷を利用する方法もあるが、単に自由膨
脹によつて得た寒冷であるためその効果はさした
るものではない。 For example, the starting method for a completely low-pressure air separation device that uses a regenerative heat exchanger and uses an expander to generate refrigeration is to pass feed air compressed to approximately 5 kg/cm 2 through the regenerative heat exchanger. After that, it is adiabatically expanded in an expander to generate refrigeration and returned to the regenerative heat exchanger to cool the vessel. Once the regenerative heat exchanger has been cooled to a certain extent, part of the generated cold and feed air is introduced into the rectification tower supercooler or liquefier, etc., and by cooling these etc., the entire equipment is cooled. Normally, the feed air introduced into the rectification column is liquefied, and the necessary conditions for rectification and separation are satisfied before steady operation begins. In this startup method, an expansion machine that is normally used only during startup is installed to increase the amount of cold generation, but because the expansion machine has a small processing capacity for the amount of raw air, the excess raw air is After being compressed, it expanded freely and was released into the atmosphere.
This not only means that the compression power is not used at all and is wasted, but also causes harmful effects due to the noise generated during free expansion into the atmosphere, and countermeasures are needed for this. For this reason, there is a method in which the surplus of the compressed raw air is allowed to freely expand within the device instead of being freely expanded into the atmosphere, and the resulting cold is used, but since the cold obtained is simply obtained by free expansion, The effect is not significant.
本発明はこのように従来の起動法における圧力
エネルギーの無駄を無くすことによつて寒冷の増
加を図り、起動時間の短縮化を可能としたもので
あり、以下にその実施例を図によつて説明する。 In this way, the present invention aims to increase cooling by eliminating the waste of pressure energy in the conventional startup method, thereby making it possible to shorten the startup time. explain.
圧縮機１にて圧縮された原料空気は、管２より
冷却器３に入り圧縮熱を除去した後、管４より切
換弁５のうちの５ｂを介して再生式熱交換器６を
通り、戻り低温ガスにより冷却される。再生式熱
交換器６を導出した原料空気は管７、逆止弁８
ａ、管９および１０を流れた後、分岐され約30％
の原料空気は、管１１、弁１２、管１３および弁
１４を介して膨脹タービン１５に導入されほぼ大
気圧まで断熱膨脹し寒冷を発生する。断熱膨脹し
た低温空気は弁１６，１７、管１８を経て過冷器
１９を通り、更に管２０より液化器２１を流れた
後、管２２を介してエゼクター２３に吸引され
る。 The raw air compressed by the compressor 1 enters the cooler 3 through the pipe 2 to remove the heat of compression, and then passes through the regenerative heat exchanger 6 through the switching valve 5b from the pipe 4 and returns. Cooled by low temperature gas. The raw air led out of the regenerative heat exchanger 6 is passed through a pipe 7 and a check valve 8.
a, After flowing through pipes 9 and 10, it is branched and about 30%
The raw material air is introduced into the expansion turbine 15 through the pipe 11, valve 12, pipe 13, and valve 14, and is adiabatically expanded to approximately atmospheric pressure to generate refrigeration. The adiabatically expanded low-temperature air passes through valves 16, 17 and pipe 18, passes through subcooler 19, and further flows through pipe 20 to liquefier 21, and is then sucked into ejector 23 via pipe 22.
一方管１０にて分岐された残りの原料空気は、
管２４、弁２５よりエゼクター２３頂部に導入さ
れ、該エゼクター２３で断熱的に膨脹し寒冷を発
生するが、この過程で液化器２１より管２２を介
して供給される低温空気を吸引する。エゼクター
２３で合流された低温空気は、管２６より逆止弁
８ｂを通り管２７を経て再生式熱交換器６を逆流
して原料空気を冷却した後、管２８、切換弁５ｄ
を経て管２９より大気へ放出される。 On the other hand, the remaining raw material air branched at the pipe 10 is
It is introduced into the top of the ejector 23 through a pipe 24 and a valve 25, where it expands adiabatically to generate cold. During this process, low-temperature air supplied from the liquefier 21 through the pipe 22 is sucked. The low-temperature air combined in the ejector 23 passes through the check valve 8b from the pipe 26, passes through the pipe 27, and flows back through the regenerative heat exchanger 6 to cool the raw air.
It is then released into the atmosphere from a pipe 29.
冷却が進行し、再生式熱交換器６の冷端部温度
が低下し、温端部温度との温度差が大きくなつて
くると、膨脹タービン１５へ導入する空気を管３
０、弁３１を介して複精溜塔３２の下部に導入し
た後、管３３より導出せしめ管３４を介して再生
式熱交換器６の冷端部に導入する。再生式熱交換
器６の冷端部を逆流し向流する原料空気を冷却し
て昇温した空気は、管３５、弁３６を経て前記管
１３、弁１４を通り膨脹タービン１５に導入さ
れ、断熱膨脹した後、過冷器１９、液化器２１を
経てエゼクター２３に吸引される。 As cooling progresses and the temperature at the cold end of the regenerative heat exchanger 6 decreases and the temperature difference between it and the temperature at the warm end increases, the air to be introduced into the expansion turbine 15 is transferred to the pipe 3.
0. After being introduced into the lower part of the double rectification column 32 via the valve 31, it is led out from the pipe 33 and introduced into the cold end of the regenerative heat exchanger 6 via the pipe 34. The air whose temperature has been increased by cooling the feed air flowing countercurrently through the cold end of the regenerative heat exchanger 6 is introduced into the expansion turbine 15 through the pipe 35 and valve 36, and then through the pipe 13 and valve 14. After adiabatically expanding, it passes through a subcooler 19 and a liquefier 21 and is sucked into an ejector 23.
更に冷却が進行して複精溜塔３２の下部塔底部
に液体空気が溜出すると、管３７より過冷器１９
を通し弁３８で膨脹した後上部塔に導入し該塔内
を冷却する。この低温空気は、上部筒頂部より管
３９を介して導出され弁４０を経て管１８を流れ
る膨脹タービン１５を出た空気と合流するが、複
精溜塔３２内の各棚段に液溜出がみられ、精溜条
件がととのうと定常運転操作に移行する。なお、
管４１、弁４２は定常運転時における損失寒冷補
給系路。管４３、弁４４は還流液体窒素の供給系
路であり、又管４５は製品酸素ガスの流路であ
り、複精溜塔３２の上部塔より導出され、再生式
熱交換器６を逆流して原料空気を冷却した後、管
４６、弁４７を介して採取される。 When cooling further progresses and liquid air is distilled out at the bottom of the lower column of the double rectification column 32, it is transferred from the pipe 37 to the subcooler 19.
After being expanded at the valve 38, it is introduced into the upper column and the inside of the column is cooled. This low-temperature air is led out from the top of the upper cylinder through a pipe 39, passes through a valve 40, flows through a pipe 18, and joins with the air exiting the expansion turbine 15. is observed, and once the rectification conditions have been adjusted, the process will shift to steady operation. In addition,
The pipe 41 and the valve 42 are a cold loss replenishment system during steady operation. The pipe 43 and valve 44 are supply lines for reflux liquid nitrogen, and the pipe 45 is a flow path for product oxygen gas, which is led out from the upper column of the double rectification column 32 and flows back through the regenerative heat exchanger 6. After cooling the raw air, it is collected through a pipe 46 and a valve 47.
以上の説明から理解できるように本発明方法
は、膨脹タービン１５に導入されない圧縮空気
（以下駆動用空気という）をエゼクター２３に導
びいて膨脹せしめると共に、膨脹タービン１５に
て膨脹した空気（以下タービン空気という）をエ
ゼクター２３に吸引せしめるようにしたことを特
徴としたものである。即ち、駆動用空気がエゼク
ター２３で膨脹する際のエゼクター効果を利用し
てタービン空気を吸引せしめ、膨脹タービン１５
の背圧を下げることによつて寒冷発生量の増加を
図つたものである。本発明方法を酸素発生量
35000m3／ｈの全低圧式空気分離装置に適用した
例を以下に示す。 As can be understood from the above description, in the method of the present invention, compressed air that is not introduced into the expansion turbine 15 (hereinafter referred to as driving air) is guided to the ejector 23 and expanded, and the air expanded in the expansion turbine 15 (hereinafter referred to as the turbine air) is guided to the ejector 23 and expanded. This device is characterized in that the ejector 23 sucks air (referred to as air). That is, by utilizing the ejector effect when the driving air is expanded in the ejector 23, the turbine air is sucked into the expansion turbine 15.
The aim is to increase the amount of cold generated by lowering the back pressure of the The amount of oxygen generated by the method of the present invention
An example of application to a 35000m 3 /h total low pressure air separation device is shown below.
全空気量 185000m3／ｈ
駆動用空気量 118000 〃
タービン空気量 67000 〃
膨脹タービン入口空気圧力 ５Kg／cm2
〃 入口温度 −150℃
断熱効果 85％
以上の場合において膨脹タービンの出口圧力を
約0.15Kg／cm2とすることが可能であるので寒冷発
生量を11.5kal／m3とすることができる。従来方
法においては膨脹タービンの出口圧力は通常0.4
Kg／cm2であり、得られる寒冷量は10.22kal／m3で
あるから膨脹タービンの出口圧力を0.25Kg／cm2下
げることができ、かつ1.28kal／m3の寒冷発生量
の増加をもたらす。従つて、従来方法に比し
85800kal／ｈの寒冷増加となり、これは通常必要
とされている起動時間である48時間を約５時間短
縮せしめることができる。Total air volume 185000m 3 /h Driving air volume 118000 〃 Turbine air volume 67000 〃 Expansion turbine inlet air pressure 5Kg/cm 2 〃 Inlet temperature -150℃ Insulation effect In cases of 85% or more, the expansion turbine outlet pressure is approximately 0.15Kg. /cm 2 , so the cold generation amount can be 11.5kal/m 3 . In conventional methods, the outlet pressure of the expansion turbine is usually 0.4
Kg/ cm2 , and the amount of refrigeration obtained is 10.22kal/ m3 , so the outlet pressure of the expansion turbine can be lowered by 0.25Kg/ cm2 , and the amount of refrigeration generated increases by 1.28kal/ m3 . . Therefore, compared to the conventional method,
This results in a cooling increase of 85,800 kal/h, which can reduce the normally required start-up time of 48 hours by about 5 hours.
図面は本発明の一実施例を示す工程図である。
６……再生式熱交換器、１５……膨脹タービ
ン、１１，１３，２２，２４……管、１４，１
７，２５……弁、２３……エゼクター、３２……
複精溜塔。
The drawings are process diagrams showing one embodiment of the present invention. 6... Regenerative heat exchanger, 15... Expansion turbine, 11, 13, 22, 24... Pipes, 14, 1
7, 25... Valve, 23... Ejector, 32...
Multiple distillation tower.
Claims (1)
の起動時に、圧縮原料空気の一部を膨脹機又は膨
脹タービン等の膨脹機関に導入し、膨脹せしめて
寒冷を発生すると共に、前記圧縮原料空気の残部
をエゼクターに導入して膨脹せしめ、得られたエ
ゼクター効果により前記膨脹機関で膨脹した空気
を吸引することにより膨脹機関の背圧を低下せし
めることを特徴とする空気分離装置の起動方法。1. When starting up an air separation device that separates air by liquefaction rectification, a part of the compressed raw air is introduced into an expansion machine such as an expansion machine or an expansion turbine, and is expanded to generate refrigeration, and the compressed raw air is A method for starting an air separation device, characterized in that the remaining portion is introduced into an ejector and expanded, and the resulting ejector effect sucks the air expanded by the expansion engine, thereby reducing the back pressure of the expansion engine.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16894579A JPS5691171A (en) | 1979-12-25 | 1979-12-25 | Method of starting air separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16894579A JPS5691171A (en) | 1979-12-25 | 1979-12-25 | Method of starting air separator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5691171A JPS5691171A (en) | 1981-07-23 |
| JPS648269B2 true JPS648269B2 (en) | 1989-02-13 |
Family
ID=15877440
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP16894579A Granted JPS5691171A (en) | 1979-12-25 | 1979-12-25 | Method of starting air separator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5691171A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0454882U (en) * | 1990-09-18 | 1992-05-11 | ||
| JP2006274954A (en) * | 2005-03-30 | 2006-10-12 | Toyota Motor Corp | Waste heat energy recovery device |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102654350B (en) * | 2012-04-24 | 2015-03-11 | 本钢板材股份有限公司 | Method for starting oxygen making unit |
-
1979
- 1979-12-25 JP JP16894579A patent/JPS5691171A/en active Granted
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0454882U (en) * | 1990-09-18 | 1992-05-11 | ||
| JP2006274954A (en) * | 2005-03-30 | 2006-10-12 | Toyota Motor Corp | Waste heat energy recovery device |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5691171A (en) | 1981-07-23 |
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