JPS6113557B2 - - Google Patents
Info
- Publication number
- JPS6113557B2 JPS6113557B2 JP54055737A JP5573779A JPS6113557B2 JP S6113557 B2 JPS6113557 B2 JP S6113557B2 JP 54055737 A JP54055737 A JP 54055737A JP 5573779 A JP5573779 A JP 5573779A JP S6113557 B2 JPS6113557 B2 JP S6113557B2
- Authority
- JP
- Japan
- Prior art keywords
- heat exchanger
- temperature
- nitrogen gas
- expander
- air
- 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
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Description
【発明の詳細な説明】
本発明は、原料空気中の水分および炭酸ガスを
除去するため、可逆熱交換器を使用した全低圧式
空気分離装置において、装置の寒冷を補償する膨
脹機の処理流体に複式精留塔の下塔の窒素ガスを
使用し、膨脹機で断熱膨脹した窒素ガスを製品ガ
ス窒素として可逆熱交換器を通して取出すように
した全低圧式空気分離装置に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention provides a total low-pressure air separation device using a reversible heat exchanger to remove moisture and carbon dioxide from feed air, and the processing fluid of the expander compensates for the cooling of the device. This invention relates to a total low-pressure air separation device in which nitrogen gas from the lower column of a double rectification column is used, and the nitrogen gas adiabatically expanded in an expander is taken out as product gas nitrogen through a reversible heat exchanger.
従来、全低圧式空気分離装置の膨脹機の処理流
体として、複式精留塔の下塔の窒素ガスを使用す
る場合には、膨脹機の寒冷発生量を大きくするた
め、下塔より取出した窒素ガスを上塔の圧力まで
断熱膨脹させ、膨脹機出口の窒素ガスは上塔から
の製品窒素や廃窒素ガスに混入する方法がとられ
ており、膨脹機出口の窒素ガスをそのまま製品と
して取出す場合でも、可逆熱交換器の入口温度条
件に調整するための単独の熱交換器とその自動制
御装置が必要とされていた。 Conventionally, when using nitrogen gas from the lower column of a double rectification column as the processing fluid for the expander of a total low-pressure air separation device, in order to increase the amount of refrigeration produced by the expander, the nitrogen gas extracted from the lower column was A method is used in which the gas is adiabatically expanded to the pressure in the upper column, and the nitrogen gas at the outlet of the expander is mixed with the product nitrogen or waste nitrogen gas from the upper column.When the nitrogen gas at the outlet of the expander is taken out as a product as it is. However, there was a need for a separate heat exchanger and its automatic controller to adjust to the inlet temperature conditions of the reversible heat exchanger.
近年、窒素の需要は各方面で増大しており、そ
の使用目的も新しい方式が採用されるようになつ
てきている。一般に全低圧式空気分離装置では、
製品窒素ガスの圧力は上塔から取出す場合は100
〜500mmAq程度である。加圧窒素の必要な場合は
下塔から直接窒素ガスを取出し、４〜５Kg/cm2Ｇ
の状態で供給することもできる。この場合はその
分に見合うだけ原料空気を増す必要があり、動力
的に不利となる。最近、使用目的によつて、窒素
ガスの圧力を0.5〜２Kg/cm2Ｇの比較的低圧の加圧
状態で採取する空気分離装置の要求がでてきてい
る。 In recent years, the demand for nitrogen has increased in various fields, and new methods are being adopted for its use. Generally, in all low pressure air separation equipment,
The pressure of the product nitrogen gas is 100 when taken out from the upper tower.
~500mmAq. If pressurized nitrogen is required, take out nitrogen gas directly from the lower column and use it at 4 to 5 kg/cm 2 G.
It can also be supplied in this state. In this case, it is necessary to increase the raw material air by an amount corresponding to that amount, which is disadvantageous in terms of power. Recently, there has been a demand for an air separation device that collects nitrogen gas at a relatively low pressurized state of 0.5 to 2 kg/cm 2 G depending on the purpose of use.
このような要求の場合、従来の全低圧式空気分
離装置では、上塔から窒素ガスを取出す方法では
別に窒素圧縮機が必要であり、下塔から直接取出
す方法では圧力が必要以上に高く、動力損失が大
きくなるため、下塔の窒素ガスを膨脹機を通し、
余分な圧力エネルギーを膨脹機で断熱膨脹させ、
寒冷を有効に利用して必要な圧力で取出すように
するのが最良の方法である。 In the case of such requirements, in conventional all-low-pressure air separation equipment, a separate nitrogen compressor is required to extract nitrogen gas from the upper column, and a method to extract nitrogen gas directly from the lower column results in unnecessarily high pressure and power consumption. Since the loss will be large, the nitrogen gas in the lower tower is passed through an expander.
Excess pressure energy is adiabatically expanded using an expansion machine,
The best way is to make effective use of the cold and extract the material at the required pressure.
可逆熱交換器を使用する全低圧式空気分離装置
においては、窒素ガスの温度は、可逆熱交換器で
の炭酸ガス昇華の問題があるため、ある一定の温
度に制御することが必要である。 In a total low pressure air separation device using a reversible heat exchanger, it is necessary to control the temperature of nitrogen gas to a certain constant temperature because of the problem of sublimation of carbon dioxide gas in the reversible heat exchanger.
一般に、膨脹機の出口温度は可逆熱交換器の入
口温度条件と一致することはまれであり、可逆熱
交換器入口温度条件と一致させるためには、膨脹
機出口に熱交換器が必要で、更に、窒素ガス温度
を制御する自動制御装置も必要になる。 Generally, the outlet temperature of the expander rarely matches the inlet temperature condition of the reversible heat exchanger, and in order to match the inlet temperature condition of the reversible heat exchanger, a heat exchanger is required at the outlet of the expander. Furthermore, an automatic control device for controlling the nitrogen gas temperature is also required.
また、装置の運転条件によつては、膨脹機の出
口温度は可逆熱交換器の入口温度条件より常に低
温であるとは限らず、必要以上に高温であること
もあり得るため、場合によつては２種類の熱交換
器を別々に設置するか、または、流体を高温と低
温の２種類流せるようなものにする必要がある。 Also, depending on the operating conditions of the equipment, the outlet temperature of the expander is not always lower than the inlet temperature of the reversible heat exchanger, and may be higher than necessary. In this case, it is necessary to install two types of heat exchangers separately, or to use one that can flow two types of fluid: high temperature and low temperature.
全低圧式空気分離装置の膨脹機の出口温度は、
膨脹機の出口圧力または処理流体の多少により温
度が変化する。即ち、出口圧力が低いと低温にな
り、高いと高温となる。また、処理流体が多い場
合は低温となり、少ないと高温となる。しかし
て、装置は使用端の目的によつて運転条件が変化
するため、これらすべての条件を満足させる必要
がある。 The outlet temperature of the expander of the total low pressure air separation equipment is
The temperature changes depending on the outlet pressure of the expander or the amount of processing fluid. That is, if the outlet pressure is low, the temperature will be low, and if the outlet pressure is high, the temperature will be high. Further, when there is a large amount of processing fluid, the temperature becomes low, and when there is little, the temperature becomes high. Since the operating conditions of the device vary depending on the purpose of use, it is necessary to satisfy all of these conditions.
本発明の目的は、膨脹機の出口温度条件のいか
んにかかわらず、一つの熱交換器で、しかも特別
な自動制御装置なしに可逆熱交換器の入口温度条
件を達成させるようにしたものである。 The object of the present invention is to achieve the inlet temperature condition of a reversible heat exchanger with one heat exchanger, regardless of the outlet temperature condition of the expander, and without any special automatic control device. .
本発明は、膨脹機出口の窒素ガスを、上塔から
の廃窒素ガス通路に設置されている熱交換器に導
くための導管を設け、更に熱交換器の内部に廃窒
素ガスと並流として窒素ガスを流す通路を設け、
膨脹機出口の窒素ガス温度が低過ぎる時は空気で
昇温し、高過ぎる場合は廃窒素で冷却できるよう
にしたものである。また、窒素ガス流路は廃窒素
と平行流としているため、特別な温度制御装置な
しで必要な温度に設定できるようにしたものであ
る。 The present invention provides a conduit for guiding the nitrogen gas at the outlet of the expander to a heat exchanger installed in the waste nitrogen gas passage from the upper tower, and further provides a conduit for guiding the nitrogen gas at the outlet of the expander to a heat exchanger installed in the waste nitrogen gas passage from the upper tower, and further creates a conduit inside the heat exchanger in parallel flow with the waste nitrogen gas. Provide a passageway for flowing nitrogen gas,
When the nitrogen gas temperature at the outlet of the expander is too low, air is used to raise the temperature, and when it is too high, waste nitrogen is used to cool it down. Furthermore, since the nitrogen gas flow path is in parallel flow with the waste nitrogen, it is possible to set the required temperature without a special temperature control device.
以下、本発明の一実施例を図面をもとに詳細に
説明する。 Hereinafter, one embodiment of the present invention will be described in detail with reference to the drawings.
圧縮され、冷却された原料空気は、導管１１よ
り可逆熱交換器１で低温の分離ガスと熱交換し、
空気中の水分および炭酸ガスを析出除去され、飽
和温度近くまで冷却されて導管１２より複式精留
塔の下塔２に吹込まれる。下塔２に吹込まれた原
料空気は、粗精留されて窒素と液体空気に分離さ
れ、液体窒素は導管１３、膨脹弁１４を通つて、
複式精留塔の上塔３の上部に還流液として供給さ
れる。下塔２の液体空気は導管１５、過冷却器
６、膨脹弁５、導管１６を通つて上塔３の中間に
吹込まれる。上塔３に送られた液体窒素および液
体空気は、上塔３で精留分離により酸素と廃窒素
に分離され、酸素は上塔３の下部から導管１７、
可逆熱交換器１を通り、原料空気と熱交換してほ
ぼ常温まで温度回復し、導管１８を通つて製品と
して使用端に供給される。 The compressed and cooled raw material air is passed through a conduit 11 to a reversible heat exchanger 1 where it exchanges heat with low-temperature separated gas.
Moisture and carbon dioxide in the air are precipitated and removed, cooled to near the saturation temperature, and blown into the lower column 2 of the double rectification column through the conduit 12. The raw air blown into the lower column 2 is crudely rectified and separated into nitrogen and liquid air, and the liquid nitrogen passes through a conduit 13 and an expansion valve 14.
It is supplied as a reflux liquid to the upper part of the upper column 3 of the double rectification column. The liquid air in the lower column 2 is blown into the middle of the upper column 3 through the conduit 15, the subcooler 6, the expansion valve 5 and the conduit 16. The liquid nitrogen and liquid air sent to the upper column 3 are separated into oxygen and waste nitrogen by rectification separation in the upper column 3, and the oxygen is passed from the lower part of the upper column 3 to a conduit 17,
It passes through the reversible heat exchanger 1, undergoes heat exchange with the raw material air, recovers the temperature to approximately room temperature, and is supplied to the end of use as a product through the conduit 18.
一方、廃窒素は上塔３の上部から導管１９、過
冷却器６を通つて下塔２からの液体空気と熱交換
して温度上昇し、更に導管２０より熱交換器７に
導かれる。熱交換器７には、従来からの空気分離
装置でとられている導管１２の空気の一部を液化
するための通路の他に、膨脹機８の出口窒素ガス
温度を調節するための通路が設けられている。熱
交換器７で昇温された廃窒素ガスは、導管２１よ
り可逆熱交換器１に導かれ、原料空気と交互に周
期的に切換えられる流路を通つて空気と熱交換
し、常温まで昇温すると同時に熱交換器に析出付
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２２より大気に放出される。製品窒素ガ
スは、下塔２の上部からガス窒素として導管２３
より抜出され、一部は導管２４より可逆熱交換器
１の再熱窒素ガスとして使用され、空気と熱交換
後導管２５より可逆熱交換器１をバイパスする導
管２６の残りの窒素ガスと合流し、導管２７より
装置の寒冷を発生させる膨脹機８に導かれる。膨
脹機８には一般に膨脹タービンが使用されてお
り、窒素の圧力的エネルギーを外部仕事にし、分
離装置全体の寒冷を補償している。 On the other hand, the waste nitrogen passes from the upper part of the upper column 3 through a conduit 19 and the subcooler 6, exchanges heat with the liquid air from the lower column 2, increases its temperature, and is further led to the heat exchanger 7 through a conduit 20. The heat exchanger 7 includes a passage for adjusting the nitrogen gas temperature at the outlet of the expander 8, in addition to a passage for liquefying a part of the air in the conduit 12, which is used in a conventional air separation device. It is provided. The waste nitrogen gas heated in the heat exchanger 7 is led to the reversible heat exchanger 1 through the conduit 21, exchanges heat with the air through a flow path that is alternately switched with the raw material air, and is raised to room temperature. At the same time as heating, moisture and carbon dioxide in the air deposited on the heat exchanger are sublimated and released into the atmosphere through the conduit 22. The product nitrogen gas is passed from the upper part of the lower column 2 to the conduit 23 as gas nitrogen.
A part of the gas is extracted from the pipe 24 and used as reheated nitrogen gas in the reversible heat exchanger 1, and after heat exchange with air, it is combined with the remaining nitrogen gas in the pipe 26 that bypasses the reversible heat exchanger 1 through the pipe 25. The air is then guided through a conduit 27 to an expander 8 that generates refrigeration for the device. An expansion turbine is generally used in the expander 8, which converts the pressure energy of the nitrogen into external work and compensates for the cooling of the entire separator.
膨脹機８で製品窒素ガスの必要圧力まで断熱膨
脹した窒素ガスは低温となり、導管２８より熱交
換器７に導かれ、高温側の原料空気または低温側
の廃窒素と熱交換して導管２９より可逆熱交換器
１に導かれ、原料空気と熱交換することによつて
常温まで温度回復し、導管３０より製品ガスとし
て使用端へ送給される。この場合、可逆熱交換器
１で空気中の水分および炭酸ガスを熱交換器を閉
塞させることなく昇華除去するためには、低温分
離ガスの入口温度をある一定条件に常に制御して
やることが必要である。このため、従来の空気分
離装置では、精留塔からの戻り分離ガス通路には
過冷却器６と一緒に熱交換器７が付属されてお
り、原料空気の一部を導管１２から分岐して導管
３１より熱交換器７に導き、空気を液化し、空気
の飽和温度を利用して戻りガスの温度を一定温度
に制御している。 The nitrogen gas that has been adiabatically expanded to the required pressure of the product nitrogen gas in the expander 8 becomes low temperature, is led to the heat exchanger 7 through the conduit 28, exchanges heat with the raw material air on the high temperature side or the waste nitrogen on the low temperature side, and is then passed through the conduit 29. The gas is guided to the reversible heat exchanger 1, and the temperature is recovered to room temperature by exchanging heat with the raw material air, and the gas is sent to the end of use as a product gas through the conduit 30. In this case, in order to sublimate and remove moisture and carbon dioxide from the air in the reversible heat exchanger 1 without clogging the heat exchanger, it is necessary to constantly control the inlet temperature of the low-temperature separated gas to a certain constant condition. be. For this reason, in conventional air separation equipment, a heat exchanger 7 is attached to the return separation gas passage from the rectification column together with a supercooler 6, and a part of the raw air is branched from the conduit 12. The air is guided through a conduit 31 to a heat exchanger 7, where the air is liquefied, and the temperature of the return gas is controlled to a constant temperature using the saturation temperature of the air.
膨脹機８で断熱膨脹し、規定値以下の低温にな
つた窒素ガスの昇温については、従来の空気の飽
和温度を利用した液化器の原理がそのまま適用さ
れるが、膨脹機８の出口窒素ガスを製品として加
圧状態で取出す場合は、出口温度が可逆熱交換器
１の入口規定温度条件より高くなり、従来の空気
との熱交換器ではその目的を達成できない。 To raise the temperature of the nitrogen gas that has been adiabatically expanded in the expander 8 and has reached a low temperature below the specified value, the principle of a conventional liquefier that uses the saturation temperature of air is applied as is. When gas is taken out as a product under pressure, the outlet temperature becomes higher than the specified temperature condition at the inlet of the reversible heat exchanger 1, and the conventional heat exchanger with air cannot achieve this purpose.
本発明では、熱交換器７に製品窒素ガスを廃窒素
と並流として流す通路が設置されているため、上
記のように膨脹機８出口の窒素ガス温度が高い場
合には、廃窒素と熱交換して冷却される。また、
通路が廃窒素と並流となつているため、廃窒素温
度より低下する心配がなく、熱交換器７の出口温
度は空気の飽和温度で制限されるため、高くなり
過ぎる心配もない。In the present invention, since the heat exchanger 7 is provided with a passage that allows the product nitrogen gas to flow in parallel with the waste nitrogen, when the nitrogen gas temperature at the outlet of the expander 8 is high as described above, the waste nitrogen and the heat It is replaced and cooled. Also,
Since the passage is in parallel flow with the waste nitrogen, there is no fear that the temperature will drop below the waste nitrogen temperature, and since the outlet temperature of the heat exchanger 7 is limited by the saturation temperature of the air, there is no fear that it will become too high.
以上述べたように、本発明によれば、膨脹機出
口の窒素ガス温度の高低のいかんにかかわらず、
常に一定の温度で可逆熱交換器へ戻りガスを導く
ことができ、熱交換器の追加や流体の切換などを
必要とせず、しかも特別な温度制御装置なしで目
的を達成させることができる。 As described above, according to the present invention, regardless of whether the nitrogen gas temperature at the expander outlet is high or low,
Return gas can always be guided to the reversible heat exchanger at a constant temperature, and there is no need to add a heat exchanger or switch fluids, and moreover, the purpose can be achieved without a special temperature control device.
図面は本発明による全低圧式空気分離装置の一
実施例を示す系統図である。
１…可逆熱交換器、２…複式精留塔の下塔、３
…複式精留塔の上塔、４，５…膨脹弁、６…過冷
却器、７…熱交換器、８…膨脹機、１１〜３１…
導管。
The drawing is a system diagram showing an embodiment of a total low pressure air separation apparatus according to the present invention. 1... Reversible heat exchanger, 2... Lower column of double rectification column, 3
... Upper tower of the double rectification column, 4, 5... Expansion valve, 6... Supercooler, 7... Heat exchanger, 8... Expansion machine, 11-31...
conduit.
Claims (1)
ため可逆熱交換器を用い、複式精留塔上塔より抜
出した廃窒素ガスの温度を、可逆熱交換器で炭酸
ガスを昇華できる温度まで原料空気の一部と熱交
換させて昇温する熱交換器を備え、装置の寒冷を
補償する膨脹機の処理流体に複式精留塔下塔の窒
素ガスを用い、膨脹機で断熱膨脹した窒素ガスを
可逆熱交換器を通して製品窒素ガスとして取出す
ようにした全低圧式空気分離装置において、前記
熱交換器に膨脹機出口の窒素ガスを廃窒素ガスと
並流として流す通路を設けたことを特徴とする全
低圧式空気分離装置。1 A reversible heat exchanger is used to remove moisture and carbon dioxide from the feed air, and the temperature of the waste nitrogen gas extracted from the upper column of the double rectification column is raised to a temperature at which carbon dioxide can be sublimed using the reversible heat exchanger. It is equipped with a heat exchanger that raises the temperature by exchanging heat with a part of the equipment, and uses nitrogen gas from the lower column of the double rectification column as the processing fluid of the expander that compensates for the coldness of the equipment. A total low-pressure air separation device in which nitrogen gas is extracted as a product through a heat exchanger, characterized in that the heat exchanger is provided with a passage through which nitrogen gas at the outlet of the expander flows in parallel with waste nitrogen gas. Low pressure air separation equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5573779A JPS55150472A (en) | 1979-05-09 | 1979-05-09 | Full low pressure type air separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5573779A JPS55150472A (en) | 1979-05-09 | 1979-05-09 | Full low pressure type air separator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS55150472A JPS55150472A (en) | 1980-11-22 |
| JPS6113557B2 true JPS6113557B2 (en) | 1986-04-14 |
Family
ID=13007159
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5573779A Granted JPS55150472A (en) | 1979-05-09 | 1979-05-09 | Full low pressure type air separator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS55150472A (en) |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3340697A (en) * | 1964-05-06 | 1967-09-12 | Hydrocarbon Research Inc | Heat exchange of crude oxygen and expanded high pressure nitrogen |
| JPS5241223A (en) * | 1975-09-23 | 1977-03-30 | Tatsuko Nishimoto | Method of attracting and killing termites |
-
1979
- 1979-05-09 JP JP5573779A patent/JPS55150472A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS55150472A (en) | 1980-11-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0524785B1 (en) | Air separation | |
| US4582519A (en) | Gas-liquefying system including control means responsive to the temperature at the low-pressure expansion turbine | |
| CN108387068A (en) | Stream backed expansion nitrogen making machine is pressurized after oxygen-enriched | |
| US2918801A (en) | Process and apparatus for separating gas mixtures | |
| US2568223A (en) | Process and apparatus for extracting oxygen from atmospheric air | |
| JPS6113557B2 (en) | ||
| US4299607A (en) | Process for recovering nitrogen in low pressure type air separation apparatus | |
| JP3703943B2 (en) | Method and apparatus for producing low purity oxygen | |
| JP4408211B2 (en) | Pressure adjusting device for liquefied natural gas tank and pressure adjusting method thereof | |
| CN109564061A (en) | For being used by low temperature air separating with variable liquid yield and power come the method and apparatus that generates air gas | |
| JPS6354991B2 (en) | ||
| JP3026091B2 (en) | Air liquefaction separation device and start-up method thereof | |
| JP3065968B2 (en) | Air liquefaction separation device and air liquefaction separation method | |
| JP3213848B2 (en) | Nitrogen production apparatus and control method thereof | |
| JP2512041B2 (en) | Operation control method for cryogenic refrigerator | |
| JPS58108381A (en) | Method of controlling temperature of reversible heat exchanger for air separator | |
| JP2967427B2 (en) | Air separation method and apparatus suitable for demand fluctuation | |
| JPH0814459B2 (en) | Air liquefaction separation method | |
| JPH0210356B2 (en) | ||
| JPH03160294A (en) | Supercooling method of liquefied nitrogen in air liquefier/separator | |
| JPH0114510B2 (en) | ||
| JPH0437353B2 (en) | ||
| JPS6323468B2 (en) | ||
| JPS6113152B2 (en) | ||
| JPH029279B2 (en) |