JPH04110382U - air separation equipment - Google Patents
air separation equipmentInfo
- Publication number
- JPH04110382U JPH04110382U JP1175691U JP1175691U JPH04110382U JP H04110382 U JPH04110382 U JP H04110382U JP 1175691 U JP1175691 U JP 1175691U JP 1175691 U JP1175691 U JP 1175691U JP H04110382 U JPH04110382 U JP H04110382U
- Authority
- JP
- Japan
- Prior art keywords
- gas
- argon
- column
- air
- liquid
- 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.)
- Pending
Links
- 238000000926 separation method Methods 0.000 title claims description 8
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims abstract description 80
- 229910052786 argon Inorganic materials 0.000 claims abstract description 40
- 239000007789 gas Substances 0.000 claims abstract description 39
- 239000007788 liquid Substances 0.000 claims abstract description 19
- 238000007664 blowing Methods 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 5
- 238000011084 recovery Methods 0.000 abstract description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 18
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 229910001873 dinitrogen Inorganic materials 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000003990 capacitor Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
(57)【要約】
【目的】粗アルゴン塔のブローガス中のアルゴンを回収
することによりアルゴンガスの回収率を高くする。
【構成】粗アルゴン塔６のブローガスを液体空気と熱交
換させる分縮器９を設置する。
【効果】粗アルゴン塔のブローガス中のアルゴン濃度を
約３分の一にすることができる。
(57) [Summary] [Purpose] To increase the recovery rate of argon gas by recovering argon from the blow gas of the crude argon column. [Structure] A dephlegmator 9 is installed to exchange heat between the blow gas from the crude argon column 6 and liquid air. [Effect] The argon concentration in the blow gas from the crude argon column can be reduced to about one-third.
Description
【０００１】0001
本考案は深冷分離式空気分離装置にかかり、特にアルゴン回収率を高めるのに 好適な空気分離装置に関するものである。 This invention applies to cryogenic air separation equipment, especially for increasing the argon recovery rate. The present invention relates to a suitable air separation device.
【０００２】0002
従来、空気分離装置においてアルゴンを採取する場合、図３に示すように精留 塔２の低圧塔の中部より抽気されたフィードアルゴンガス中に含まれる窒素ガス 等の非凝縮性のガスは粗アルゴン塔６頂部に滞留するため、次第に凝縮器の伝熱 面積を減少させる。このため、粗アルゴン塔６頂部に設けられたブロー用の導管 より非凝縮性のガスを大気に放出し、凝縮器内部での非凝縮性のガスの濃縮を防 止していた。（特開昭５４−１１６３８５号参照） 又、このブローガスを回収する目的で、液体窒素とブローガスを熱交換させ凝 縮させる凝縮器を設ける方法が提案されている。（特開昭５４−１１６３８４号 参照） Conventionally, when extracting argon in an air separation device, rectification is performed as shown in Figure 3. Nitrogen gas contained in the feed argon gas extracted from the middle of the low pressure column of column 2 Since non-condensable gases such as Reduce area. For this reason, a blowing conduit installed at the top of the crude argon column 6 Releases more non-condensable gases to the atmosphere and prevents non-condensable gases from concentrating inside the condenser. It had stopped. (Refer to Japanese Patent Application Laid-open No. 54-116385) In addition, in order to recover this blow gas, liquid nitrogen and blow gas are condensed by heat exchange. A method of providing a condenser for condensation has been proposed. (Unexamined Japanese Patent Publication No. 54-116384 reference)
【０００３】0003
上記従来技術では、原料空気中のアルゴンガスの回収率を増加した場合、フィ ードアルゴンガス中の非凝縮性ガス濃度が増加するに連れて、ブローガス量を増 加させる必要があった。このため、原料空気中のアルゴンの一部を放出すること になり、従って、アルゴンの回収率を増加させる場合妨げとなっていた。 In the above conventional technology, when the recovery rate of argon gas in the feed air is increased, As the non-condensable gas concentration in the argon gas increases, the amount of blow gas increases. I needed to add it. For this reason, some of the argon in the feed air must be released. Therefore, increasing the argon recovery rate was a hindrance.
【０００４】 又、液体窒素を使用する場合にはその消費量が増加するため、余分な液体窒素の 消費量が増加するという問題があった。0004 Also, when using liquid nitrogen, its consumption increases, so avoid using excess liquid nitrogen. There was a problem of increased consumption.
【０００５】 本考案の目的は、液体窒素など他の低温熱源を使用すること無く、粗アルゴン 塔頂部からのブローガス量を減少させることにより、原料空気中のアルゴンガス の回収率を上げることにある。[0005] The purpose of this invention is to generate crude argon gas without using other low-temperature heat sources such as liquid nitrogen. By reducing the amount of blow gas from the top of the tower, argon gas in the feed air can be removed. The goal is to increase the collection rate.
【０００６】[0006]
上記目的は、液体空気との熱交換を行なう分縮効果を有するブローガスの分縮 器を設けることにより達成される。 The above purpose is to decompose blow gas, which has a decomposition effect that exchanges heat with liquid air. This is achieved by providing a container.
【０００７】[0007]
粗アルゴン塔に供給される断熱膨張させた後の液体空気とブローガスが分縮器 で熱交換され、それによりブローガス中のアルゴンが凝縮して大気に放出される アルゴンガスを減少させることができる。 The liquid air and blow gas after adiabatic expansion are supplied to the crude argon column and sent to the dephlegmator. The argon in the blow gas is condensed and released into the atmosphere. Argon gas can be reduced.
【０００８】[0008]
以下、本考案の一実施例を図１により説明する。 An embodiment of the present invention will be described below with reference to FIG.
【０００９】 空気分離装置に供給された空気は、空気熱交換器１で液化点付近まで冷却され た後、大部分は精留塔２の中圧塔に送られる。一部分の空気は空気熱交換器１の 中間部より抽気され、膨張タービン５で膨張させ必要な寒冷を発生させた後、精 留塔２の低圧塔に供給される。[0009] The air supplied to the air separation device is cooled to near the liquefaction point in air heat exchanger 1. After that, most of it is sent to the medium pressure column of rectification column 2. A portion of the air is transferred to air heat exchanger 1. Air is extracted from the middle section, expanded by the expansion turbine 5 to generate the necessary cooling, and then refined. It is fed to the low pressure column of distillation column 2.
【００１０】 精留塔２の中圧塔で窒素と高酸素濃度液体空気に粗精留された空気は、各々過 冷却器３，４で過冷却された後精留塔２低圧塔に送られ、ここで高純酸素として 分離精製される。アルゴン分離のためのフィードガスは精留塔２低圧塔の中部よ り抽気されて粗アルゴン塔６底部に供給され、ここで約９７％の粗アルゴンに精 製される。粗アルゴン塔６を上昇してきたガスを凝縮し下降液を確保するために 必要な低温熱源として、液体空気の一部が粗アルゴン塔６頂部に設けられたコン デンサ８に供給されている。0010 The air crudely rectified into nitrogen and high oxygen concentration liquid air in the medium pressure column of rectification column 2 is filtered. After being subcooled in coolers 3 and 4, it is sent to the rectification column 2 low pressure column, where it is purified as high-purity oxygen. Separated and purified. Feed gas for argon separation is supplied from the middle of the rectification column 2 low pressure column. The crude argon is extracted and supplied to the bottom of the crude argon column 6, where approximately 97% of the crude argon is purified. Manufactured. In order to condense the gas rising in the crude argon column 6 and secure the descending liquid. As a necessary low-temperature heat source, a portion of the liquid air is supplied to a condenser installed at the top of the crude argon column 6. It is supplied to the capacitor 8.
【００１１】 本系統において、フィードガス中に含まれている主に窒素ガス等の非凝縮性の ガスは、粗アルゴン塔６頂部の導管を経由して大気に放出されるが、この放出ガ ス中の窒素濃度は、粗アルゴン塔６頂部に設置されたコンデンサ８内部の液体空 気の飽和温度と同一飽和温度となる混合ガス組成となる。[0011] In this system, mainly non-condensable gas such as nitrogen gas contained in the feed gas is used. The gas is released to the atmosphere via a conduit at the top of the crude argon column 6; The nitrogen concentration in the gas is determined by the liquid space inside the condenser 8 installed at the top of the crude argon column 6. This results in a mixed gas composition that has the same saturation temperature as the saturation temperature of air.
【００１２】 この時、液体空気の組成はコンデンサ８内の気液平衡関係より約７０％酸素と なっており、この飽和温度（８８．６゜Ｋ）と同一の飽和温度となるブローガス 中の窒素濃度は約１０％となる。0012 At this time, the composition of the liquid air is approximately 70% oxygen based on the vapor-liquid equilibrium relationship in the condenser 8. The blow gas has the same saturation temperature as this saturation temperature (88.6°K). The nitrogen concentration inside is about 10%.
【００１３】 従って、フィードガス中に混入した窒素ガスを粗アルゴン塔６より放出するた めには、混入した窒素ガスの約９倍のアルゴンを捨てることになる。[0013] Therefore, in order to release the nitrogen gas mixed in the feed gas from the crude argon column 6, In order to achieve this, approximately 9 times as much argon as nitrogen gas must be discarded.
【００１４】 本考案ではこの放出ガス中のアルゴン濃度を低くするため、分縮器９を設置し 、ブローガスを液体空気と熱交換させ放出ガス中のアルゴンを凝縮させている。[0014] In this invention, a decentralizer 9 is installed in order to lower the argon concentration in this released gas. , the blow gas is heat exchanged with liquid air to condense the argon in the discharged gas.
【００１５】 分縮器９に供給された液体空気は、断熱膨張した直後では入口の組成とほとん ど同一であるため、約８３゜Ｋまで冷却されている。このため、ブローガス中の アルゴンガスは分縮され、大部分が凝縮しアルゴン濃度を約３５％まで低下させ ることができる。この結果、大気に放出するアルゴンガス量を約３分の１に低下 することができる。[0015] Immediately after adiabatic expansion, the liquid air supplied to the demultiplexer 9 has a composition that is almost the same as that at the inlet. Since they are the same, they are cooled to about 83°K. For this reason, during blow gas Argon gas is fractionated and most of it condenses, reducing the argon concentration to about 35%. can be done. As a result, the amount of argon gas released into the atmosphere has been reduced to approximately one-third. can do.
【００１６】 又、分縮器９を粗アルゴン塔６のコンデンサ８の液溜め内部の空間に設置した 場合でも同様の効果を得ることができ、その実施例を図２に示す。図２において 、粗アルゴン塔６のコンデンサ８に供給された液体空気は入口配管の下部に設け られた液受けに供給され、分縮器９に供給される。[0016] In addition, a decentralizer 9 was installed in the space inside the liquid reservoir of the condenser 8 of the crude argon column 6. A similar effect can be obtained even in the case of the present invention, and an example thereof is shown in FIG. In Figure 2 The liquid air supplied to the condenser 8 of the crude argon column 6 is provided at the bottom of the inlet pipe. The liquid is then supplied to the demultiplexer 9.
【００１７】[0017]
本考案によれば、他の低温熱源を使用すること無く、粗アルゴン塔頂部からの ブローガス量を減少させることにより、原料空気中のアルゴンガスの回収率を上 げることができる。 According to the present invention, crude argon is extracted from the top of the column without using any other low-temperature heat source. By reducing the amount of blow gas, the recovery rate of argon gas in the feed air is increased. can be given.
【図１】本考案の一実施例を示す系統図である。FIG. 1 is a system diagram showing an embodiment of the present invention.
【図２】本考案の他の実施例を示す系統図である。FIG. 2 is a system diagram showing another embodiment of the present invention.
【図３】従来技術を示す系統図である。FIG. 3 is a system diagram showing a prior art.
１…空気熱交換器、２…精留塔、３，４…過冷却器、５
…膨張タービン、６…粗アルゴン塔、７…主凝縮器、８
…コンデンサ、９…分縮器。1... Air heat exchanger, 2... Rectification column, 3, 4... Supercooler, 5
…expansion turbine, 6…crude argon column, 7…main condenser, 8
...capacitor, 9...demultiplexer.
Claims (1)
アルゴン塔の頂部に設けられたブロー用の導管にブロー
ガスを液体空気と熱交換させる分縮器を設けたことを特
徴とする空気分離装置。1. An air separation apparatus using a cryogenic separation method, characterized in that a blowing conduit provided at the top of a crude argon column is provided with a dephlegmator for exchanging blow gas with liquid air. Device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1175691U JPH04110382U (en) | 1991-03-06 | 1991-03-06 | air separation equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1175691U JPH04110382U (en) | 1991-03-06 | 1991-03-06 | air separation equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH04110382U true JPH04110382U (en) | 1992-09-24 |
Family
ID=31900847
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1175691U Pending JPH04110382U (en) | 1991-03-06 | 1991-03-06 | air separation equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH04110382U (en) |
-
1991
- 1991-03-06 JP JP1175691U patent/JPH04110382U/en active Pending
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