JPS6357713B2 - - Google Patents
Info
- Publication number
- JPS6357713B2 JPS6357713B2 JP3169182A JP3169182A JPS6357713B2 JP S6357713 B2 JPS6357713 B2 JP S6357713B2 JP 3169182 A JP3169182 A JP 3169182A JP 3169182 A JP3169182 A JP 3169182A JP S6357713 B2 JPS6357713 B2 JP S6357713B2
- Authority
- JP
- Japan
- Prior art keywords
- inert gas
- separation device
- air separation
- liquefied
- source
- 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
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 31
- 239000011261 inert gas Substances 0.000 claims description 26
- 239000003949 liquefied natural gas Substances 0.000 claims description 24
- 238000000926 separation method Methods 0.000 claims description 20
- 229910052757 nitrogen Inorganic materials 0.000 claims description 15
- 238000000034 method Methods 0.000 claims description 13
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 8
- 238000004064 recycling Methods 0.000 claims description 8
- 229910052786 argon Inorganic materials 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims 1
- 239000001301 oxygen Substances 0.000 claims 1
- 229910052760 oxygen Inorganic materials 0.000 claims 1
- 238000005057 refrigeration Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 description 6
- 230000006835 compression Effects 0.000 description 4
- 238000007906 compression Methods 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 238000004172 nitrogen cycle Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000010420 art technique Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- NBVXSUQYWXRMNV-UHFFFAOYSA-N fluoromethane Chemical compound FC NBVXSUQYWXRMNV-UHFFFAOYSA-N 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Description
本発明は、空気分離装置において外部冷熱源を
有効に利用できる経済的な方法に関するものであ
る。
液化天然ガス（以下LNGと記す）の使用に際
しては、これをガス化することが必要であるが、
ガス化時に発生する冷熱の有効利用が種々試みら
れている。それらの一つとして、空気を液化精留
して液体酸素、液体窒素等の液体製品を採取する
空気分離装置の外部冷熱源として利用することが
知られている。
たとえば、特公昭49−45054号、特公昭49−
40353号、特開昭56−34083号等の公報には、
LNGの冷熱を原料空気の冷却に利用する方法が
開示され、特公昭52−41224号、特公昭53−15993
号、特公昭50−1359号、特公昭46−18125号等の
公報にはリサイクル窒素の冷却、液化にLNGの
冷熱を利用する方法が開示されている。また特公
昭46−16081号、特公昭46−19685号、特公昭46−
20123号等の公報には原料空気とリサイクル窒素
の両者をLNGによつて冷却する方法が示されて
いる。
空気分離装置に必要な冷熱を供給するための窒
素サイクルを採用する場合、窒素の圧縮、膨張に
よる冷熱の発生が行われるが、低温ガスを圧縮す
る方が消費電力を低減できるので、前記発明のう
ち、特公昭53−15993号、特公昭50−1359号、特
公昭46−18125号、特公昭46−16081号、特公昭46
−19685号、特公昭４−20123号各公報記載の発明
では、LNG又は空気分離装置で分離された低温
ガス等で冷却された低温窒素を圧縮する、いわゆ
る低温圧縮を採用して動力費の節減を図つてい
る。
さらに特公昭56−34785号公報には、LNGによ
つてリサイクル窒素を冷却するほか、他の冷媒
（フロン）を冷却し、これを原料空気の予冷に用
いる方法が開示されている。
本発明は、これらの先行技術に比してさらに
LNGの冷熱を十分に利用し、しかも外部冷熱源
利用サイクルに必要な動力費を極小にすることが
できる空気分離装置における外部冷熱源利用方法
を提供するものである。
以下、本発明の１実施例を示す図によつて本発
明の方法を説明する。
図において、１は空気分離装置であるが、この
詳細は本発明の主要部ではなので、図示並びに説
明を省略する。空気分離装置１において、それに
必要な冷熱を与えた不性ガスは導管２によつて取
出され、リサイクル熱交換器３に送われ、ここに
おいて後述する液化不活性ガスによりLNGの温
度付近まで冷却されて導管４によつて圧縮機５に
導かれる。低温不活性ガスは圧縮機５により後述
するLNGとの熱交換で液化するに必要な圧力ま
で低温圧縮され、導管６に送られて、後述する導
管１５からの低温不活性ガスと合流して導管７よ
りLNG熱交換器８に供給される。LNG熱交換器
８では、導管９から導入されるLNGによつて低
温不活性ガスは液化され、LNGは気化されて導
管１０から導出され、使用先に送られる。LNG
交換器８で液化された液化不活性ガスは導管１１
によつて取出されて空気分離装置１に送られ、こ
こで必要な冷熱を供給した後に再び導管２から取
出されてリサイクルする。液化不活性ガスの一部
は導管１１から導管１２に分岐し、ポンプ１３に
よつて昇圧され導管１４によりリサイクル熱交換
器３に供給される。リサイクル熱交換器３に送ら
れた液化不活性ガスは前記のように導管２から導
入される不活性ガスを冷却して自らは気化し、低
温不活性ガスとなり導管１５によつて取出され、
前記のように導管６の低温不活性ガスと合流す
る。
上記の如く本発明の操作において窒素をリサイ
クルガスとして用いた場合の各ラインにおける流
体、流量、圧力及び温度の一例を表記すれば下記
のとおりである。尚、下表の例は製品液体O2、
N2及びAr計10000Nm3／ｈの時の数値である。
The present invention relates to an economical method of making effective use of an external cold source in an air separation device. When using liquefied natural gas (hereinafter referred to as LNG), it is necessary to gasify it.
Various attempts have been made to effectively utilize the cold energy generated during gasification. As one of these methods, it is known to use air as an external cold source for an air separation device that collects liquid products such as liquid oxygen and liquid nitrogen by liquefaction rectification of air. For example, Special Publication No. 49-45054, Special Publication No. 49-49-
Publications such as No. 40353 and Japanese Unexamined Patent Publication No. 56-34083,
A method of using the cold energy of LNG to cool feed air was disclosed, and was published in Japanese Patent Publication Nos. 52-41224 and 15993.
Japanese Patent Publication No. 50-1359, Japanese Patent Publication No. 46-18125, etc. disclose methods of utilizing the cold energy of LNG for cooling and liquefying recycled nitrogen. Also, Special Publication No. 16081, Special Publication No. 19685, Special Publication No. 46-1968,
Publications such as No. 20123 show a method of cooling both raw air and recycled nitrogen using LNG. When a nitrogen cycle is adopted to supply the cold heat necessary for an air separation device, the cold heat is generated by compressing and expanding nitrogen. However, since power consumption can be reduced by compressing low-temperature gas, the invention Among them, Special Publication No. 53-15993, Special Publication No. 50-1359, Special Publication No. 18125, Special Publication No. 46-16081, Special Publication No. 16081, Special Publication No. 1972.
-19685 and Japanese Patent Publication No. 4-20123, the inventions reduce power costs by compressing low-temperature nitrogen cooled with LNG or low-temperature gas separated by an air separation device, so-called low-temperature compression. We are trying to Furthermore, Japanese Patent Publication No. 56-34785 discloses a method in which, in addition to cooling recycled nitrogen with LNG, another refrigerant (fluorocarbon) is cooled, and this is used to pre-cool raw material air. The present invention has further advantages over these prior art techniques.
The present invention provides a method for utilizing an external cold source in an air separation device that can fully utilize the cold energy of LNG and minimize the power cost required for the external cold source utilization cycle. The method of the present invention will be explained below with reference to figures showing one embodiment of the present invention. In the figure, numeral 1 indicates an air separation device, but since the details are not the main part of the present invention, illustration and explanation will be omitted. In the air separation device 1, the inert gas that has been given the necessary cold heat is taken out through the conduit 2 and sent to the recycling heat exchanger 3, where it is cooled to near the temperature of LNG by liquefied inert gas, which will be described later. and is led to a compressor 5 by a conduit 4. The low-temperature inert gas is low-temperature compressed by the compressor 5 to the pressure necessary for liquefaction through heat exchange with LNG, which will be described later, and sent to the conduit 6, where it joins with the low-temperature inert gas from the conduit 15, which will be described later, to form the conduit. 7, the LNG is supplied to the LNG heat exchanger 8. In the LNG heat exchanger 8, the low-temperature inert gas is liquefied by the LNG introduced from the conduit 9, and the LNG is vaporized and led out from the conduit 10 and sent to a user. LNG
The liquefied inert gas liquefied in the exchanger 8 is transferred to the conduit 11
The air is taken out from the pipe 2 and sent to the air separation device 1, where the necessary cold heat is supplied, and then taken out again from the conduit 2 for recycling. A portion of the liquefied inert gas is branched from conduit 11 to conduit 12, pressurized by pump 13, and supplied to recycle heat exchanger 3 via conduit 14. The liquefied inert gas sent to the recycling heat exchanger 3 cools the inert gas introduced from the conduit 2 as described above, vaporizes itself, becomes a low-temperature inert gas, and is taken out through the conduit 15.
As before, it joins the cold inert gas in conduit 6. An example of the fluid, flow rate, pressure and temperature in each line when nitrogen is used as the recycle gas in the operation of the present invention as described above is as follows. The examples in the table below are for product liquid O 2 ,
The values are when the total amount of N 2 and Ar is 10,000 Nm 3 /h.
【表】
このように、本発明の方法では、リサイクル不
活性ガスはリサイクル熱交換器３においてLNG
温度付近まで冷却されているので圧縮機５では圧
縮に要するエネルギーの少い低温圧縮が行われ、
またLNG熱交換器８で液化された液化不活性ガ
スの一部もポンプ１３によつて昇圧し、リサイク
ルさせているので、リサイクルに要するエネルギ
ーを極小に抑えることができる。即ち、従来公知
の秀れたこの種方式に比べて電力消費量は1/4以
下となつた。
LNG熱交換器８でのLNGと低温不活性ガスと
の熱交換は、不活性ガスが圧縮機５でその熱交換
によつて液化するに必要な圧力まで圧縮されてい
るし、圧縮前にリサイクル熱交換器３でLNG温
度付近まで冷却されているので、LNGの冷熱を
十分に利用することができる。
リサイクルする不活性ガスとしては、窒素及び
アルゴンが工業的に使用される。
窒素をリサイクルガスとして用いる場合、液体
窒素の一部は導管１１から空気分離装置１に導入
されてそれに必要な冷熱を供給する。その態様は
前記のように種々公知のものがあるが、一般には
液体窒素が精留塔に還流液として吹込まれ、それ
と同量の窒素ガスが精留塔から取出されて原料空
気の冷却等に使用された後、導管２によつて空気
分離装置１から導出されて窒素サイクルを形成し
ている。
アルゴンをリサイクルガスとして用いる場合に
は、たとえば本出願人が先に出願した特願昭55−
64105号に開示されているように、空気分離装置
１内に導入された液化アルゴンによつてリサイク
ル窒素を冷却液化して製品液体窒素や精留塔還流
液としたり、またこのような熱交換によつて気化
した低温アルゴンガスで原料空気を冷却すること
ができる。[Table] In this way, in the method of the present invention, the recycled inert gas is LNG in the recycling heat exchanger 3.
Since it has been cooled to around the temperature, the compressor 5 performs low-temperature compression, which requires less energy for compression.
In addition, a portion of the liquefied inert gas liquefied in the LNG heat exchanger 8 is also pressurized by the pump 13 and recycled, so that the energy required for recycling can be kept to a minimum. In other words, the power consumption is less than 1/4 of that of conventionally known and superior systems of this type. In the heat exchange between LNG and low-temperature inert gas in the LNG heat exchanger 8, the inert gas is compressed to the pressure necessary for liquefaction in the compressor 5 by heat exchange, and is recycled before compression. Since the heat exchanger 3 cools the LNG to near the temperature, the cold energy of the LNG can be fully utilized. Nitrogen and argon are used industrially as inert gases to be recycled. If nitrogen is used as the recycle gas, a portion of the liquid nitrogen is introduced into the air separation device 1 via conduit 11 to supply it with the necessary cold heat. There are various known methods as mentioned above, but in general, liquid nitrogen is blown into the rectification tower as a reflux liquid, and the same amount of nitrogen gas is taken out from the rectification tower to cool the raw air, etc. After being used, it is led out of the air separation device 1 by a conduit 2 to form a nitrogen cycle. When using argon as a recycled gas, for example, the patent application filed in 1983 by the applicant
As disclosed in No. 64105, recycled nitrogen is cooled and liquefied by liquefied argon introduced into the air separation device 1 to become product liquid nitrogen or rectification column reflux liquid, or for such heat exchange. The raw material air can then be cooled with the vaporized low-temperature argon gas.
添付図面は本発明の一例を示すフローシートで
あり、図中、１は空気分離装置を省略して示し、
２，４，６，７，９，１０，１１，１２，１４及
び１５は導管、３はリサイクル熱交換器、５は圧
縮機、８はLNG熱交換器、１３はポンプをそれ
ぞれ示す。
The attached drawing is a flow sheet showing an example of the present invention, and in the drawing, 1 shows the air separation device omitted,
2, 4, 6, 7, 9, 10, 11, 12, 14 and 15 are conduits, 3 is a recycling heat exchanger, 5 is a compressor, 8 is an LNG heat exchanger, and 13 is a pump, respectively.
Claims (1)
として液状で製出する空気分離装置に他の外部冷
熱源を利用する方法において、空気分離装置から
導出されたリサイクル不活性ガスを液化された不
活性ガスの一部と間接熱交換して冷却し、次いで
外部冷熱源との熱交換により液化するに必要な圧
力まで低温圧縮し、この圧縮低温不活性ガスを外
部冷熱源との間接熱交換により液化し、この液化
不活性ガスの一部をポンプにより所要圧昇圧して
前記リサイクル熱交換器に冷熱源として供給し、
ここで気化した低温不活性ガスを前記圧縮機で圧
縮された低温不活性ガスと合流させるとともに、
前記液化不活性ガスの他の部分を空気分離装置に
導入してこれに必要な寒冷を供給した後、再びリ
サイクル不活性ガスとして空気分離装置から導出
する空気分離装置における外部冷熱源を利用する
方法。 ２ リサイクル不活性ガスが窒素である特許請求
の範囲第１項記載の空気分離装置における外部冷
熱源を利用する方法。 ３ リサイクル不活性ガスがアルゴンである特許
請求の範囲第１項記載の空気分離装置における外
部冷熱源を利用する方法。 ４ 他の冷熱源が液化天然ガスである特許請求の
範囲第１項記載の空気分離装置における外部冷熱
源を利用する方法。[Scope of Claims] 1. In a method in which an external cold source is used in an air separation device that liquefies and rectifies air to produce products such as oxygen and nitrogen mainly in liquid form, recycling derived from the air separation device The inert gas is cooled by indirect heat exchange with a portion of the liquefied inert gas, then cold compressed by heat exchange with an external cold source to the pressure required for liquefaction, and this compressed low temperature inert gas is transferred to an external source. Liquefied by indirect heat exchange with a cold heat source, a part of this liquefied inert gas is boosted to a required pressure by a pump and supplied to the recycling heat exchanger as a cold heat source,
The vaporized low-temperature inert gas is combined with the low-temperature inert gas compressed by the compressor, and
Another part of the liquefied inert gas is introduced into the air separation device to supply the necessary refrigeration thereto, and then the other portion is led out of the air separation device as a recycled inert gas, using an external cold source in the air separation device. . 2. A method of utilizing an external cold source in an air separation device according to claim 1, wherein the recycled inert gas is nitrogen. 3. A method of utilizing an external cold source in an air separation device according to claim 1, wherein the recycled inert gas is argon. 4. A method of utilizing an external cold source in an air separation device according to claim 1, wherein the other cold source is liquefied natural gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3169182A JPS58150786A (en) | 1982-03-02 | 1982-03-02 | Method of utilizing external cold heat source in air separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3169182A JPS58150786A (en) | 1982-03-02 | 1982-03-02 | Method of utilizing external cold heat source in air separator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58150786A JPS58150786A (en) | 1983-09-07 |
| JPS6357713B2 true JPS6357713B2 (en) | 1988-11-11 |
Family
ID=12338094
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3169182A Granted JPS58150786A (en) | 1982-03-02 | 1982-03-02 | Method of utilizing external cold heat source in air separator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58150786A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0789014B2 (en) * | 1987-07-28 | 1995-09-27 | テイサン株式会社 | Method of using external cold heat source in air separation device |
| US5139547A (en) * | 1991-04-26 | 1992-08-18 | Air Products And Chemicals, Inc. | Production of liquid nitrogen using liquefied natural gas as sole refrigerant |
| US5141543A (en) * | 1991-04-26 | 1992-08-25 | Air Products And Chemicals, Inc. | Use of liquefied natural gas (LNG) coupled with a cold expander to produce liquid nitrogen |
-
1982
- 1982-03-02 JP JP3169182A patent/JPS58150786A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS58150786A (en) | 1983-09-07 |
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