JPS6354991B2 - - Google Patents
Info
- Publication number
- JPS6354991B2 JPS6354991B2 JP576480A JP576480A JPS6354991B2 JP S6354991 B2 JPS6354991 B2 JP S6354991B2 JP 576480 A JP576480 A JP 576480A JP 576480 A JP576480 A JP 576480A JP S6354991 B2 JPS6354991 B2 JP S6354991B2
- Authority
- JP
- Japan
- Prior art keywords
- temperature
- heat exchanger
- expander
- air
- conduit
- 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
- 230000002441 reversible effect Effects 0.000 claims description 24
- 239000007788 liquid Substances 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 15
- 238000000926 separation method Methods 0.000 claims description 12
- 238000011084 recovery Methods 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 33
- 239000007789 gas Substances 0.000 description 30
- 229910001873 dinitrogen Inorganic materials 0.000 description 13
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 11
- 229910052757 nitrogen Inorganic materials 0.000 description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 239000001569 carbon dioxide Substances 0.000 description 5
- 239000002699 waste material Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Description
【発明の詳細な説明】
本発明は空気分離装置の膨張機出口ガスの温度
制御方法に係り、特に原料空気中の水分および炭
酸ガスを除去するため可逆熱交換器を設けてある
全低圧式空気分離装置の寒冷を補償する膨張機出
口ガスの温度を制御するのに好適な温度制御方法
に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for controlling the temperature of expander exit gas of an air separation device, and particularly relates to a method for controlling the temperature of expander outlet gas of an air separation device, and particularly relates to a method for controlling the temperature of expander outlet gas of an air separation device, and particularly to a total low-pressure air system equipped with a reversible heat exchanger to remove moisture and carbon dioxide from raw air. The present invention relates to a temperature control method suitable for controlling the temperature of expander outlet gas to compensate for the coldness of the separation device.
従来、全低圧式空気分離装置の膨張機出口ガス
は、精留塔上塔中部に吹込んだり、上塔からの廃
ガスまたは製品窒素に混入させて、熱交換器で可
逆式熱交換器必要入口温度に調整する方法がとら
れていた。 Conventionally, the expander outlet gas of a total low-pressure air separation device is blown into the middle of the upper column of the rectification column, or mixed with waste gas or product nitrogen from the upper column, and a reversible heat exchanger is required. A method was used to adjust the inlet temperature.
ところで、最近、膨張機の処理流体として下塔
の窒素ガスを使用し、膨張機から出た窒素ガスを
可逆式熱交換器の切換に影響のない通路を通して
製品として取出す方式がしばしばとられるように
なつてきている。 By the way, recently, a method has often been adopted in which nitrogen gas from the lower column is used as the processing fluid for the expander, and the nitrogen gas discharged from the expander is taken out as a product through a passage that does not affect the switching of the reversible heat exchanger. I'm getting used to it.
しかし、膨張機出口ガス温度は、装置の寒冷量
に応じて変化するのが普通であるため、膨張機出
口ガス温度を熱交換器で可逆式熱交換器の入口温
度条件に合うように制御してやることが必要であ
る。 However, since the expander outlet gas temperature usually changes depending on the amount of refrigeration in the equipment, the expander outlet gas temperature is controlled by a heat exchanger to match the inlet temperature condition of the reversible heat exchanger. It is necessary.
この方法としては、膨張機出口に２つの熱交換
器を設け、そのうちの１つは、膨張機出口ガス温
度が可逆式熱交換器入口温度条件より低い場合の
昇温のための熱交換器とし、他の１つは、高過ぎ
た場合の冷却用熱交換器として用いる方法があ
る。 In this method, two heat exchangers are installed at the outlet of the expander, one of which is used as a heat exchanger to raise the temperature when the expander outlet gas temperature is lower than the reversible heat exchanger inlet temperature condition. Another method is to use it as a cooling heat exchanger when the temperature is too high.
しかし、熱交換器を２つ設け、高温流体と低温
流体を切換えて、膨張機出口ガス温度を制御する
ことは、設備高となるばかりでなく、自動温度制
御装置として複雑なものとなるので、実際には採
用されるに至つていない。 However, installing two heat exchangers and switching between high-temperature fluid and low-temperature fluid to control the expander outlet gas temperature not only increases the equipment cost, but also makes the automatic temperature control system complicated. It has not actually been adopted.
実際に採用されている例としては、上塔からの
廃窒素ラインに設備されている液化器に別通路を
設け、下塔空気の飽和温度が変らないということ
を利用して、自動制御なしで使つているものがあ
る。しかし、この方法は、装置がそれほど大形の
ものでなければ問題ないが、大形装置では、熱交
換器が気体と気体との熱交換であるため、伝熱面
積を増大しなければならず、価格的に不利とな
る。 As an example of actual use, a separate passage is installed in the liquefier installed in the waste nitrogen line from the upper tower, and the saturation temperature of the air in the lower tower does not change. There is something I use. However, this method has no problems unless the equipment is very large, but in large equipment, the heat transfer area must be increased because the heat exchanger exchanges heat between gases. , which is disadvantageous in terms of price.
本発明は上記に鑑みてなされたもので、その目
的とするところは、膨張機出口ガス温度の高低に
かかわらず、膨張機出口ガス温度を１つの熱交換
機を用いて可逆式熱交換器必要入口温度に制御す
ることができる空気分離装置の膨張機出口ガスの
温度制御方法を提供することにある。 The present invention has been made in view of the above, and its purpose is to adjust the temperature of the expander outlet gas to a reversible heat exchanger using a single heat exchanger, regardless of whether the expander outlet gas temperature is high or low. An object of the present invention is to provide a method for controlling the temperature of expander outlet gas of an air separation device, which can control the temperature.
本発明の特徴は、膨張機の出口側に熱交換器を
設け、上記膨張機の出口ガス温度の高低に応じて
上記出口ガスと精留塔の下塔へ供給する空気また
は上記下塔の液体空気とで上記熱交換器で熱交換
させて上記膨張機出口ガス温度を可逆式熱交換器
の必要入口温度に温度制御するようにした点にあ
る。 A feature of the present invention is that a heat exchanger is provided on the outlet side of the expander, and depending on the temperature of the outlet gas of the expander, the outlet gas and the air supplied to the lower column of the rectification column or the liquid of the lower column The present invention is characterized in that the temperature of the gas at the outlet of the expander is controlled to the required inlet temperature of the reversible heat exchanger by exchanging heat with air in the heat exchanger.
以下本発明の方法の一実施例を図を用いて詳細
に説明する。 An embodiment of the method of the present invention will be described in detail below with reference to the drawings.
図は本発明の方法の実施を可能とした全低圧式
空気分離装置の系統図である。図において、圧縮
された空気は導管１より可逆式熱交換器２に供給
され、可逆式熱交換器２で低温の分離ガスとの熱
交換によつて空気中の水分および炭酸ガスが除去
された状態で空気の飽和温度近くまで冷却され、
導管３より複式精留塔の下塔４に吹込まれる。 The figure is a system diagram of a total low-pressure air separation device that makes it possible to carry out the method of the present invention. In the figure, compressed air is supplied from conduit 1 to reversible heat exchanger 2, where moisture and carbon dioxide in the air are removed by heat exchange with low-temperature separated gas. The air is cooled to near its saturation temperature,
It is blown into the lower column 4 of the double rectification column through the conduit 3.
下塔４に吹込まれた空気は粗溜され、窒素と液
体空気とに分離され、液体窒素は、導管５を通
し、上塔圧力まで膨張させた後、上塔６の上部に
還流液として供給される。 The air blown into the lower column 4 is roughly distilled and separated into nitrogen and liquid air, and the liquid nitrogen is expanded to the upper column pressure through a conduit 5 and then supplied to the upper part of the upper column 6 as a reflux liquid. be done.
下塔４の液体空気は、導管７、熱交換器８を通
し、上塔圧力まで膨張させた後、上塔６の中部に
還流液として供給される。 Liquid air in the lower column 4 passes through a conduit 7 and a heat exchanger 8, expands to the upper column pressure, and then is supplied to the middle of the upper column 6 as a reflux liquid.
上塔６に送られた液体窒素および液体空気は、
上塔６で精留分離により酸素と廃窒素に分離さ
れ、酸素は上塔６の下部から導管９、熱交換器
８、導管１０を通つて可逆式熱交換器２に至り、
ここで常温まで温度回復して導管１１から製品酸
素として取出される。 The liquid nitrogen and liquid air sent to the upper tower 6 are
Oxygen and waste nitrogen are separated by rectification in the upper column 6, and the oxygen reaches the reversible heat exchanger 2 from the lower part of the upper column 6 through a conduit 9, a heat exchanger 8, and a conduit 10.
Here, the temperature is restored to room temperature and taken out from the conduit 11 as product oxygen.
一方、廃窒素は、上塔６の上部から導管１２、
熱交換器８、導管１３を通つて可逆式熱交換器２
に導かれる。ここで廃窒素は、空気と交互に周期
的に切換えられる流路を通り、空気との熱交換に
よつて常温まで昇温されると同時に可逆式熱交換
器２の流路上に凝結付着している空気中の水分お
よび炭酸ガスを昇華させ、導管１４より大気に放
出される。 On the other hand, waste nitrogen is transferred from the upper part of the upper tower 6 to the conduit 12,
Reversible heat exchanger 2 through heat exchanger 8 and conduit 13
guided by. Here, the waste nitrogen passes through a flow path that is periodically switched alternately with air, and is heated to room temperature by heat exchange with the air, and at the same time condenses and adheres to the flow path of the reversible heat exchanger 2. Moisture and carbon dioxide in the air are sublimated and released into the atmosphere through the conduit 14.
製品窒素ガスは、下塔４の上部から導管１５よ
りガスとして抜き出され、一部は導管１６より可
逆式熱交換器２に導かれ、再熱窒素ガスとして使
用され、空気と熱交換後、導管１７を通り、バイ
パスする導管１８からの残りの窒素ガスと合流し
て、導管１９より装置の寒冷を発生させる膨張機
２０に導かれる。 The product nitrogen gas is extracted as a gas from the upper part of the lower tower 4 through a conduit 15, and a portion is led to the reversible heat exchanger 2 through a conduit 16, where it is used as reheated nitrogen gas, and after heat exchange with air, It passes through conduit 17, joins the remaining nitrogen gas from bypassing conduit 18, and is conducted by conduit 19 to expander 20, which generates refrigeration of the device.
膨張機２０としては、一般に膨張タービンが使
われており、窒素の圧力的エネルギーを外部仕事
にし、分離器の寒冷量を補償している。膨張機２
０で製品窒素ガスの必要圧力まで断熱膨張した窒
素ガスは、低温となつて導管２１より熱交換器２
２に導かれ、高温側の空気または低温側の液体空
気との熱交換によつて可逆式熱交換器２の必要冷
端温度（入口温度）に調整され、導管２３、可逆
熱交換器２を通つた後、導管２４より製品窒素ガ
スとして取出される。 An expansion turbine is generally used as the expander 20, and converts the pressure energy of nitrogen into external work to compensate for the amount of refrigeration in the separator. Expander 2
The nitrogen gas that has expanded adiabatically to the required pressure of the product nitrogen gas at zero temperature becomes low temperature and passes through the conduit 21 to the heat exchanger 2.
2, the temperature is adjusted to the required cold end temperature (inlet temperature) of the reversible heat exchanger 2 by heat exchange with air on the high temperature side or liquid air on the low temperature side, and the conduit 23 and the reversible heat exchanger 2 are After passing through, it is taken out from the conduit 24 as a product nitrogen gas.
可逆式熱交換器２で空気中の水分および炭酸ガ
スが熱交換器を閉塞させることがないように、そ
れを昇華除去するためには、低温分離ガスの入口
での温度条件をある一定の温度（約−177℃）に
制御してやることが絶対条件となる。 In order to sublimate and remove moisture and carbon dioxide in the air so that they do not block the heat exchanger in the reversible heat exchanger 2, the temperature condition at the inlet of the low-temperature separation gas must be set to a certain temperature. The absolute requirement is to control the temperature to about -177°C.
ところで、膨張機２０で断熱膨張によつて窒素
ガスが−177℃以下に下がつたときは、液化器を
設けて、下塔４に供給される空気を導いて液化さ
せることによつて、窒素ガスの温度を−177℃と
することができる。しかし、膨張機２０の出口ガ
スを加圧状態で取り出したり、大形分離装置にな
ると、膨張機２０の出口ガス温度が常に−177℃
以下となるとは限らない。場合によつては−160
℃以上となることもあり、このような温度の高い
ガスを可逆式熱交換器２に供給すると、原料空気
が十分冷却されず、炭酸ガスが除去されないまま
精留塔に供給されることになり、ドライアイスに
よる装置の閉塞事故の発生の原因になる。 By the way, when the nitrogen gas drops to -177°C or lower due to adiabatic expansion in the expander 20, a liquefier is installed to guide and liquefy the air supplied to the lower column 4, thereby converting the nitrogen gas into The temperature of the gas can be -177°C. However, if the outlet gas of the expander 20 is taken out under pressure or is used in a large separation device, the temperature of the outlet gas of the expander 20 will always be -177°C.
There is no guarantee that it will be less than that. -160 in some cases
℃ or higher, and if such high-temperature gas is supplied to the reversible heat exchanger 2, the feed air will not be sufficiently cooled and will be supplied to the rectification column without removing carbon dioxide gas. This can lead to equipment blockage accidents due to dry ice.
そこで、本発明においては、上記したように、
膨張機２０の出口側に熱交換器２２を設け、膨張
機２０からの断熱膨張によつて低温となつた窒素
ガスを導いて、高温側の空気または低温側の液体
空気と熱交換させて、可逆式熱交換器２の必要入
口温度に合うように温度制御するようにした。 Therefore, in the present invention, as described above,
A heat exchanger 22 is provided on the outlet side of the expander 20, and the nitrogen gas that has become low temperature due to adiabatic expansion from the expander 20 is guided to exchange heat with air on the high temperature side or liquid air on the low temperature side, The temperature was controlled to match the required inlet temperature of the reversible heat exchanger 2.
以下具体的に説明すると、例えば、膨張機２０
の出口ガス温度が−177℃以下の低温のときは、
温度調節装置２５により、液体空気調整弁３７を
閉止、空気調整弁２７を必要弁開度とし、下塔４
へ供給する空気を導管２６、弁２７、導管２８，
２９を通して熱交換器２２に導びく。この空気
は、熱交換器２２で膨張機２０からの窒素ガスで
冷却され、液化して導管３０より逆止弁３１、導
管３２に取付けた絞り板３３を通つて、導管３４
より下塔４に導かれる。なお、導管３４の先端
は、下塔４の底部に溜つている液体空気中に挿入
してあつて液シールするようにしてある。このよ
うにして、膨張機出口ガス温度が可逆式熱交換器
２の必要入口温度に制御される。 Specifically described below, for example, the expander 20
When the outlet gas temperature is low, below -177℃,
The temperature adjustment device 25 closes the liquid air adjustment valve 37, sets the air adjustment valve 27 to the required valve opening degree, and lowers the lower tower 4.
Conduit 26, valve 27, conduit 28,
29 to the heat exchanger 22. This air is cooled by nitrogen gas from the expander 20 in the heat exchanger 22, liquefied, and passed from the conduit 30 through the check valve 31 and the throttle plate 33 attached to the conduit 32, to the conduit 34.
You will be led to Lower Tower 4. The tip of the conduit 34 is inserted into the liquid air accumulated at the bottom of the lower column 4 to form a liquid seal. In this way, the expander outlet gas temperature is controlled to the required inlet temperature of the reversible heat exchanger 2.
反対に、膨張機２０の出口ガス温度が−177℃
より高くなつた場合は、温度調節装置２５の指令
により、弁２７を閉止、弁３７を必要弁開度とす
る。弁３７は導管３６で導管２９に、また、導管
３８で上塔６の中部に接続してあるから、弁３７
が開くと、熱交換器２２の空気側の圧力が低下
し、それまで逆止弁３１を通つて流れていた液体
空気の流れが閉止され、絞り板３３で膨張して低
温になつた下塔４の底部の液体空気が、逆に導管
３２，３０を通つて熱交換器２２に導かれる。そ
してこの液体空気は、膨張機２０からの温度の高
い出口ガスと熱交換してガス化され、導管２９，
３６、弁３７、導管３８を通つて上塔６の中部に
吹込まれる。なお、下塔４の熱交換器２２に流入
する液体空気量は、弁３７の開度によつて自動的
に制御されており、圧力による液体空気の温度変
化と流量変化で、熱交換器２２から可逆式熱交換
器２に流入する窒素ガスは、効率よく必要入口温
度に制御される。 On the other hand, the outlet gas temperature of the expander 20 is -177℃
If it becomes higher, the valve 27 is closed and the valve 37 is set to the required valve opening degree in accordance with a command from the temperature control device 25. Since the valve 37 is connected to the conduit 29 by a conduit 36 and to the middle part of the upper tower 6 by a conduit 38, the valve 37
When opened, the pressure on the air side of the heat exchanger 22 decreases, and the flow of liquid air that had previously flowed through the check valve 31 is closed, and the lower column, which has expanded at the throttle plate 33 and has become low temperature, is The liquid air at the bottom of 4 is directed back through conduits 32, 30 to heat exchanger 22. This liquid air is then gasified by exchanging heat with the high temperature outlet gas from the expander 20, and is gasified through the conduit 29,
36, valve 37, and conduit 38 into the middle of the upper tower 6. Note that the amount of liquid air flowing into the heat exchanger 22 of the lower tower 4 is automatically controlled by the opening degree of the valve 37, and the amount of liquid air flowing into the heat exchanger 22 is controlled by the temperature change and flow rate change of the liquid air due to pressure. The nitrogen gas flowing into the reversible heat exchanger 2 is efficiently controlled to the required inlet temperature.
上記したように、本発明の実施例によれば、膨
張機２０の出口側に熱交換器２２を設け、膨張機
２０出口ガス温度が低温過ぎるときは、下塔４へ
供給する空気と熱交換させ、また、高温過ぎると
きは下塔４の液体空気と熱交換させて、可逆式熱
交換器２の必要入口温度に自動的に温度制御する
ようにしたので、簡単な構成で、良好な温度制御
を行うことができる。しかも、空気分離装置の容
量に無関係に温度制御を行うことができる。 As described above, according to the embodiment of the present invention, the heat exchanger 22 is provided at the outlet side of the expander 20, and when the gas temperature at the outlet of the expander 20 is too low, heat exchanger with the air supplied to the lower column 4 is provided. In addition, when the temperature is too high, the temperature is automatically controlled to the required inlet temperature of the reversible heat exchanger 2 by exchanging heat with the liquid air in the lower tower 4, so it is possible to maintain a good temperature with a simple configuration. can be controlled. Moreover, temperature control can be performed regardless of the capacity of the air separation device.
以上説明したように、本発明によれば、１つの
熱交換器を用いて膨張機出口ガス温度を可逆式熱
交換器必要入口温度に制御することができるとい
う効果がある。 As explained above, according to the present invention, there is an effect that the expander outlet gas temperature can be controlled to the reversible heat exchanger required inlet temperature using one heat exchanger.
図は本発明の方法の一実施例を説明するための
全低圧式空気分離装置の系統図である。
１…圧縮空気導管、２…可逆式熱交換器、４…
精留塔下塔、６…精留塔上塔、１５，１６，１
７，１８，１９…製品窒素導管、２０…膨張機、
２２…熱交換器、２３…導管、２５…温度調整装
置、２６，２８，２９，３０，３２，３４，３
６，３８…導管、２７…空気調節弁、３１…逆止
弁、３３…絞り板、３７…液体空気調節弁。
The figure is a system diagram of a total low pressure air separation apparatus for explaining one embodiment of the method of the present invention. 1...Compressed air conduit, 2...Reversible heat exchanger, 4...
Fractionation column lower column, 6... Fractionation column upper column, 15, 16, 1
7, 18, 19... Product nitrogen conduit, 20... Expander,
22... Heat exchanger, 23... Conduit, 25... Temperature adjustment device, 26, 28, 29, 30, 32, 34, 3
6, 38... Conduit, 27... Air control valve, 31... Check valve, 33... Throttle plate, 37... Liquid air control valve.
Claims (1)
交換器に導いて熱回収するようにしてなる空気分
離装置の膨張機出口ガスの温度制御方法におい
て、 前記膨張機の出口側に熱交換器を設け、前記膨
張機の出口ガス温度の高低に応じて該出口ガスと
精留塔の下塔へ供給する空気または前記精留塔下
塔の液体空気とを前記熱交換器で熱交換させて前
記膨張機出口ガス温度を前記可逆式熱交換器の必
要入口温度に温度制御することを特徴とする膨張
機出口ガスの温度制御方法。[Scope of Claims] 1. A method for controlling the temperature of expander outlet gas of an air separation device, in which outlet gas of an expander for compensating for cold temperature is guided to a reversible heat exchanger for heat recovery, comprising: A heat exchanger is provided on the outlet side, and depending on the temperature of the outlet gas of the expander, the outlet gas and the air supplied to the lower column of the rectification column or the liquid air of the lower column of the rectification column are exchanged through the heat exchanger. A method for controlling the temperature of expander outlet gas, characterized in that the temperature of the expander outlet gas is controlled to a required inlet temperature of the reversible heat exchanger by exchanging heat with the expander outlet gas.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP576480A JPS56105283A (en) | 1980-01-23 | 1980-01-23 | Method of controlling temperature of outlet gas of expansion machine of air separator |
| DE3018476A DE3018476C2 (en) | 1979-05-16 | 1980-05-14 | Process and plant for the production of gaseous nitrogen |
| US06/149,630 US4299607A (en) | 1979-05-16 | 1980-05-14 | Process for recovering nitrogen in low pressure type air separation apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP576480A JPS56105283A (en) | 1980-01-23 | 1980-01-23 | Method of controlling temperature of outlet gas of expansion machine of air separator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS56105283A JPS56105283A (en) | 1981-08-21 |
| JPS6354991B2 true JPS6354991B2 (en) | 1988-10-31 |
Family
ID=11620186
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP576480A Granted JPS56105283A (en) | 1979-05-16 | 1980-01-23 | Method of controlling temperature of outlet gas of expansion machine of air separator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS56105283A (en) |
-
1980
- 1980-01-23 JP JP576480A patent/JPS56105283A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS56105283A (en) | 1981-08-21 |
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