JPH0323831B2 - - Google Patents
Info
- Publication number
- JPH0323831B2 JPH0323831B2 JP16807183A JP16807183A JPH0323831B2 JP H0323831 B2 JPH0323831 B2 JP H0323831B2 JP 16807183 A JP16807183 A JP 16807183A JP 16807183 A JP16807183 A JP 16807183A JP H0323831 B2 JPH0323831 B2 JP H0323831B2
- Authority
- JP
- Japan
- Prior art keywords
- air
- column
- heat exchanger
- oxygen
- rectification column
- 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
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 34
- 239000001301 oxygen Substances 0.000 claims description 34
- 229910052760 oxygen Inorganic materials 0.000 claims description 34
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 14
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 10
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 7
- 230000000630 rising effect Effects 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims 1
- 238000001704 evaporation Methods 0.000 description 10
- 230000008020 evaporation Effects 0.000 description 10
- 238000000034 method Methods 0.000 description 10
- 238000004519 manufacturing process Methods 0.000 description 8
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Description
本発明は空気を液化して分離する方法に関し、
特に全低圧方式によつて空気を分離し高純度の製
品酸素を経済的に製造する方法に関するものであ
る。
空気を液化して精留することによりN2、O2、
Ar等を分離する空気の液化分離装置は種々の分
野で稼働している。この種の空気液化分離装置で
は、原料空気等に対して運転条件に応じた加圧、
減圧操作を施す必要がある為、圧縮機や膨張ター
ビン等の機器の設備が不可欠である。そして空気
液化分離装置は一般に大容量のものが多く運転動
力が嵩むため製品酸素の製造コストの低減を図る
には精留効率を向上させると共に、運転動力費を
できる限り節約しなければならないとする産業上
の要請が強く、本発明者等もこの要請に対応すべ
く特に製品酸素圧送用圧縮機について鋭意検討を
行なつてきた。
従来の全低圧式空気分離による高純度酸素製造
方法（以下単に酸素製造方法という）は、主とし
て第１図に示す様な系統図に従つて行なわれてい
る。
以下の説明中、切換式熱交換器は特許請求の範
囲に記載の「主熱交換器」の一例であつて、例え
ば切替式吸着器を入口側に有する熱交換器等にも
適用可能である。第１図において原料空気は空気
過器１を通して供給され、空気圧縮機２で約５
Kg／cm2Ｇに圧縮加圧された後、アフタクーラ３で
冷却される。次いで導管５から切換式熱交換器６
に導入され、精留塔８で分離精製された戻りガス
により冷却さると共に、空気中に含まれる水分及
び炭酸ガス等が除去される。この空気は、導管７
を経て精留塔下塔（以下単に下塔という）８ｂに
導かれる。こうして下塔８ｂに導入された空気は
上昇ガスとなる一方、該下塔８ｂの頂部で凝縮し
て得られる還流液（富窒素液）に接触させて粗精
留し、下塔８ｂの頂部で富窒素液を得ると共に、
前記還流液は下塔８ｂの底部で酸素成分約30〜40
％の富酸素液体空気となる。下塔８ｂで前述の如
く粗精留された液体空気は、管路９を通つて液体
空気過冷却器１０内に導入・冷却された後、管路
１１から精留塔上塔（以下単に上塔という）８ａ
の中部へ導かれる。又下塔８ｂの頂部に貯留され
た富窒素液は管路１２を通つて液体空気過冷却器
１０内に導入・冷却された後、管路１３から上塔
８ａの上部へ導かれる。一方下塔８ｂ内を上昇す
る気体空気の一部は導管１４から抜出された後、
切換式熱交換器６の再熱回路１５に導入され、切
換式交換器６の中間温度を調整した後、調整弁１
６を経て膨張タービン１７に送られる。膨張ター
ビン１７において約0.32Kg／cm2Ｇに膨張され大気
吸込型負荷ブロワで外部仕事を取り出すことによ
つて所要寒冷を得た空気は、導管１８を経て上塔
８ａに吸込まれる。
こうして上塔８ａで分離精製された高純度酸素
成分、高純度窒素成分及び不純窒素成分は、それ
ぞれ導管１９，２０，２１よりガス状で抽気され
て切換式交換器６に送られ、前述の如く原料空気
と熱交換することによつて、常温まで温度回復を
受けた後製品として取り出され、特に酸素は導管
２２から圧縮機３０に導入して例えば約30Kg／cm2
Ｇまで加圧された後、製品酸素として回収され
る。
これに対し本発明者等は上記の従来プロセスに
おける圧縮機３０についての、製品酸素圧送用動
力の効率的な低域の可能性について種々検討を行
なつているが、圧縮機３０に導入される気化製品
酸素を別の圧縮機によることなく、即ち動力の消
費を伴わずに予め昇圧させておくことができれば
圧縮機３０についての動力消費量を効果的に低減
し得るという技術的指針の下にその様な非動力的
昇圧手段を開発すべく鋭意研究の結果、本発明を
完成したものである。
しかしてこの様な本発明の空気分離方法とは、
精留塔の外部に配置された蒸発器に酸素を液状で
導入する一方、前記精留塔下塔から抜出された気
体空気の一部を循環熱交換器に通して昇温した
後、前記膨張タービンの負荷ブロワにかけて昇圧
し、更に該昇圧空気を前記循環熱交換器に通して
冷却した後、前記蒸発器内に設置されたリボイラ
に導入して高純度液体酸素成分を気化せしめると
共に自らは液化し、気化酸素成分は上記切換式熱
交換器に送る一方、液化空気は前記精留塔下塔内
に戻す様にした点に要旨を有するものである。
以下実施例図面に基づき本発明の構成及び作用
効果を説明するが、下記実施例は単に一代表例に
過ぎないものであつて、前・後記の趣旨に沿つて
適宜変更して実施し得ることは言うまでもない。
第２図は本発明の全低圧式空気分離方法の系統
図を示し、第１図に示す従来例と基本的構成は同
一であり、同一構成のものには同一の符号を付
し、その説明は省略する。以下本実施例の特徴と
する構成を中心に説明する。
精留塔８の外部には蒸発器３１が配設され、該
蒸発器３１下部と最下底部８′ａは導管３２で連
結される。又蒸発器３１の頂部から延設された導
管３６は切換式熱交換器６と連結されている。更
に蒸発器３１には蒸発用熱交換器（以下単に蒸発
熱交という）３７が収納されており、該蒸発熱交
３７の上部と気体空気抜出用導管１４からの分岐
導管３８は循環熱交換器３９、膨張タービンの負
荷ブロワ１７ａ及びアフタクーラ４２を介して連
結されると共に、蒸発熱交３７の下部と下塔８ｂ
は導管４４で連結されている。即ち下塔８ｂから
抜出された気体空気の一部は導管３８から循環熱
交換器３９を経由して導管４０から負荷ブロワ１
７ａに導入され、更に該ブロワ１７ａを出た後ア
フタクーラ４２及び循環熱交換器３９を順次経由
して導管４３から蒸発熱交３７に送られ、ここで
液化された後導管４４から下塔８ｂ内に戻る様に
構成されている。
この様に構成された酸素製造プロセスにおい
て、上塔８ａの底部に留まる液体酸素は導管３２
を通つて蒸発器３１に供給される一方、蒸発熱交
３７には下塔８ｂから抜出された気体空気が前述
の如く導管４３から供給されるので、熱交換によ
つて蒸発器３１内の液体酸素を気化せしめると共
に自らは液化する。こうして気化された液体酸素
（以下気化酸素という）は導管３６から抜出され
て切換式熱交換器６を経由した後圧縮機３０に供
給されるが、このときの供給圧力は従来の場合に
比べて高くなつている。
即ち本発明プロセスでは上述した様に導管１４
から抜出された気体空気は膨張タービン１７の負
荷ブロワ１７ａにかけて圧縮・昇圧を受けた後で
蒸発熱交３７に供給されるので、蒸発器３１内に
おける液体酸素との熱交換による液化温度が高め
になる。従つてそれに伴う効果として液体酸素の
蒸発温度も高くすることができ、気化圧力がその
分増加する。その結果、導管３６内を輸送される
気化酸素の圧力は第１図に示す導管１９内を輸送
される従来の気化酸素圧力よりも高くなつてい
る。従つて圧縮機３０における消費動力をその分
削減することができる。従つて上塔８ａ内の上昇
ガス量は変化せず、従来プロセスと比べて上塔８
ａ内の精留条件が悪くなることはないので特に製
品酸素については十分な収率を維持することがで
きる。
一方蒸発熱交３７内で液化した空気は導管４４
から下塔８ｂ内に返送されるが、この液化分だけ
下塔８ｂ内の上昇ガス量が減少するので、下塔８
ｂについては精留条件の多少の低下が懸念され
る。しかしこの場合は製品窒素の収率が若干低下
するだけであつて製品酸素の収率には何ら影響し
ないので、製品酸素の回収を主目的とする本発明
プロセスにおいて上記構成即ち液化空気の下塔８
ｂ内への返送は何ら問題とはならない。
又図示の如く蒸発器３１を予め上塔８ａの最下
底部より十分下方に設置しておけば、蒸発器３１
に供給される液体酸素の圧力は、上塔８ａ内にお
ける液体酸素上面と蒸発器３１における液体酸素
上面との間の水頭差に相当する分だけ高くなり、
蒸発器３１内における液体酸素の気化能力を更に
強化されるので推奨構成例と言える。
尚蒸発熱交３７に昇圧空気を供給するためのプ
ロセス構成としては図示例以外に例えば第３図に
示すものでもよく、この例では下塔８ｂからの気
体空気を切換式熱交換器６の再熱回路１５を通過
せしめた後、循環熱交換器３９に通して昇温し、
これを膨張タービンの負荷ブロワ１７ａにかけて
昇圧し、更に循環熱交換器３９に通して冷却した
後の昇圧空気の一部を導管５０から蒸発熱交３７
に供給している。この構成例においても第２図例
の場合と同様の作用効果が得られることは言うま
でもない。
実施例
製造規模10000Nm3、回収酸素圧力30Kg／cm2Ｇ
の酸素製造装置について第１図に示す従来方法及
び第２図に示す本発明方法を夫々適用した場合の
製品酸素圧送動力の比較を行なつた所、第１表に
示す結果が得られた。
The present invention relates to a method for liquefying and separating air,
In particular, the present invention relates to a method for economically producing high-purity product oxygen by separating air using a completely low-pressure system. By liquefying air and rectifying it, N 2 , O 2 ,
Air liquefaction separation equipment that separates Ar, etc. is used in various fields. This type of air liquefaction separation equipment pressurizes the raw air etc. according to the operating conditions.
Since it is necessary to perform pressure reduction operations, equipment such as compressors and expansion turbines are essential. Air liquefaction separation equipment generally has a large capacity and requires a lot of operating power, so in order to reduce the production cost of product oxygen, it is necessary to improve rectification efficiency and save operating power costs as much as possible. There is a strong industrial demand, and in order to meet this demand, the inventors of the present invention have conducted intensive studies, especially regarding a compressor for pressurizing product oxygen. A conventional high-purity oxygen production method (hereinafter simply referred to as an oxygen production method) using total low-pressure air separation is mainly carried out according to a system diagram as shown in FIG. In the following explanation, the switching type heat exchanger is an example of the "main heat exchanger" described in the claims, and is also applicable to, for example, a heat exchanger having a switching type adsorber on the inlet side. . In FIG. 1, raw air is supplied through an air filter 1, and an air compressor 2
After being compressed and pressurized to Kg/cm 2 G, it is cooled in an aftercooler 3. Then from the conduit 5 to the switched heat exchanger 6
The air is cooled by the return gas that is introduced into the air and separated and purified in the rectification column 8, and moisture, carbon dioxide, and the like contained in the air are removed. This air flows through conduit 7
It is guided to the lower column of the rectification column (hereinafter simply referred to as the lower column) 8b. The air thus introduced into the lower column 8b becomes a rising gas, and is crudely rectified by being brought into contact with the reflux liquid (nitrogen-rich liquid) obtained by condensation at the top of the lower column 8b. Along with obtaining nitrogen-rich liquid,
The reflux liquid has an oxygen content of about 30 to 40 at the bottom of the lower column 8b.
% oxygen-enriched liquid air. The liquid air crudely rectified as described above in the lower column 8b is introduced into the liquid air subcooler 10 through a pipe 9 and cooled, and then sent from the pipe 11 to the upper column of the rectification column (hereinafter simply referred to as the upper column). (called the tower) 8a
guided to the middle of Further, the nitrogen-rich liquid stored at the top of the lower column 8b is introduced into the liquid air supercooler 10 through a pipe 12 and cooled, and then guided through a pipe 13 to the upper part of the upper tower 8a. On the other hand, after a part of the gaseous air rising inside the lower tower 8b is extracted from the conduit 14,
After being introduced into the reheat circuit 15 of the switching type heat exchanger 6 and adjusting the intermediate temperature of the switching type exchanger 6, the regulating valve 1
6 and is sent to an expansion turbine 17. The air, which has been expanded to approximately 0.32 kg/cm 2 G in the expansion turbine 17 and obtained the required cooling by extracting external work with an atmospheric suction type load blower, is sucked into the upper tower 8a through the conduit 18. The high-purity oxygen component, high-purity nitrogen component, and impure nitrogen component thus separated and purified in the upper column 8a are extracted in gaseous form through conduits 19, 20, and 21, respectively, and sent to the switching exchanger 6, as described above. By exchanging heat with the raw material air, the temperature is recovered to room temperature and then taken out as a product. In particular, oxygen is introduced into the compressor 30 from the conduit 22 and is heated to about 30 kg/cm 2 , for example.
After being pressurized to G, it is recovered as product oxygen. In response, the present inventors have conducted various studies on the possibility of efficient low-range power for pumping product oxygen with respect to the compressor 30 in the above-mentioned conventional process. Under the technical guidance that the power consumption of the compressor 30 can be effectively reduced if the vaporized oxygen product can be pressurized in advance without using a separate compressor, that is, without consuming power. The present invention was completed as a result of intensive research to develop such a non-powered pressure boosting means. However, the air separation method of the present invention is as follows:
Oxygen is introduced in liquid form into an evaporator placed outside the rectification column, while a part of the gaseous air extracted from the lower column of the rectification column is passed through a circulation heat exchanger to raise its temperature, and then the expansion The pressure is increased by applying it to the load blower of the turbine, and the pressurized air is cooled by passing through the circulation heat exchanger, and then introduced into the reboiler installed in the evaporator to vaporize the high-purity liquid oxygen component and liquefy it itself. However, the gist is that the vaporized oxygen component is sent to the switching heat exchanger, while the liquefied air is returned to the lower column of the rectification column. The configuration and effects of the present invention will be explained below based on the drawings of the embodiments. However, the embodiments below are merely representative examples, and the embodiments can be implemented with appropriate changes in accordance with the spirit of the above and below. Needless to say. FIG. 2 shows a system diagram of the all-low-pressure air separation method of the present invention. The basic configuration is the same as that of the conventional example shown in FIG. is omitted. The following description will focus on the feature of this embodiment. An evaporator 31 is disposed outside the rectifying column 8, and the lower part of the evaporator 31 and the lowest bottom part 8'a are connected by a conduit 32. A conduit 36 extending from the top of the evaporator 31 is connected to the switching heat exchanger 6. Further, the evaporator 31 houses an evaporation heat exchanger (hereinafter simply referred to as an evaporation heat exchanger) 37, and the upper part of the evaporation heat exchanger 37 and a branch conduit 38 from the gas air extraction conduit 14 are used for circulating heat exchange. 39, the load blower 17a of the expansion turbine, and the aftercooler 42, and the lower part of the evaporative heat exchanger 37 and the lower column 8b.
are connected by a conduit 44. That is, a part of the gaseous air extracted from the lower column 8b is sent from the conduit 38 via the circulation heat exchanger 39 and from the conduit 40 to the load blower 1.
7a, and after exiting the blower 17a, it is sent from a conduit 43 to an evaporation heat exchanger 37 via an aftercooler 42 and a circulation heat exchanger 39 in order, and after being liquefied here, it is sent from a conduit 44 into the lower column 8b. It is configured to return to In the oxygen production process configured in this way, the liquid oxygen remaining at the bottom of the upper column 8a is transferred to the conduit 32.
The gaseous air extracted from the lower column 8b is supplied to the evaporation heat exchanger 37 from the conduit 43 as described above, so that the air inside the evaporator 31 is It vaporizes liquid oxygen and liquefies itself. The liquid oxygen vaporized in this way (hereinafter referred to as vaporized oxygen) is extracted from the conduit 36 and supplied to the compressor 30 after passing through the switching heat exchanger 6, but the supply pressure at this time is lower than that in the conventional case. It's getting expensive. That is, in the process of the present invention, the conduit 14 is
The gaseous air extracted from the expansion turbine 17 is compressed and pressurized by the load blower 17a of the expansion turbine 17, and then supplied to the evaporation heat exchanger 37, so that the liquefaction temperature due to heat exchange with liquid oxygen in the evaporator 31 is increased. become. Therefore, as an accompanying effect, the evaporation temperature of liquid oxygen can also be increased, and the evaporation pressure increases accordingly. As a result, the pressure of vaporized oxygen transported within conduit 36 is higher than the conventional vaporized oxygen pressure transported within conduit 19 shown in FIG. Therefore, the power consumption in the compressor 30 can be reduced accordingly. Therefore, the amount of rising gas in the upper column 8a does not change, and compared to the conventional process, the amount of rising gas in the upper column 8a does not change.
Since the rectification conditions in a are not deteriorated, a sufficient yield can be maintained especially for the product oxygen. On the other hand, the air liquefied in the evaporative heat exchanger 37 is transferred to the conduit 44.
However, since the amount of rising gas in the lower column 8b decreases by the liquefied amount, the lower column 8
As for b, there is a concern that the rectification conditions may deteriorate somewhat. However, in this case, the yield of product nitrogen is only slightly reduced and the yield of product oxygen is not affected at all. Therefore, in the process of the present invention whose main purpose is to recover product oxygen, 8
There is no problem with sending it back to B. In addition, if the evaporator 31 is installed in advance sufficiently below the bottom of the upper column 8a as shown in the figure, the evaporator 31
The pressure of the liquid oxygen supplied to the upper column 8a increases by an amount corresponding to the water head difference between the upper surface of the liquid oxygen in the upper tower 8a and the upper surface of the liquid oxygen in the evaporator 31,
This can be said to be a recommended configuration example because the ability to vaporize liquid oxygen in the evaporator 31 is further strengthened. In addition to the illustrated example, the process configuration for supplying pressurized air to the evaporation heat exchanger 37 may be the one shown in FIG. After passing through the heat circuit 15, it is passed through a circulation heat exchanger 39 to raise the temperature,
The pressure of this air is raised by applying it to the load blower 17a of the expansion turbine, and after cooling it by passing it through the circulation heat exchanger 39, a part of the pressurized air is sent from the conduit 50 to the evaporation heat exchanger 37.
is supplied to. It goes without saying that in this configuration example, the same effects as in the example shown in FIG. 2 can be obtained. Example Production scale 10000Nm 3 , recovered oxygen pressure 30Kg/cm 2 G
The results shown in Table 1 were obtained by comparing the power for pumping product oxygen when the conventional method shown in FIG. 1 and the method of the present invention shown in FIG. 2 were applied to the oxygen production apparatus shown in FIG.
【表】
第１表から明らかな様に本発明方法による場合
は従来方法に比べて動力消費原単位が約９％以上
減少していることが計算で求められる。従つて本
発明方法によればランニングコストの大巾な節約
が期待でき、製品酸素をより安価に製造できるこ
とが明らかである。
本発明の空気分離方法は以上の様に構成される
が、要は製品酸素圧送用圧縮機に導入される気化
酸素を予め自己昇圧できるようにしたので、該圧
縮機の消費動力を刷減できることとなり、高純度
製品酸素はより安価に製造できる様になつた。又
空気分離装置の運転に要する動力を低減すること
によりいわゆる省エネルギー化を図ることができ
るので、エネルギーの節約が強く叫ばれている今
日、こうした面からの産業界に果たす役割も大き
い。[Table] As is clear from Table 1, calculations show that the method of the present invention reduces the unit power consumption by about 9% or more compared to the conventional method. Therefore, it is clear that the method of the present invention can be expected to significantly reduce running costs and produce oxygen product at a lower cost. The air separation method of the present invention is configured as described above, but the key point is that the vaporized oxygen introduced into the product oxygen pressure-feeding compressor can be self-pressurized in advance, so that the power consumption of the compressor can be reduced. As a result, high-purity product oxygen can now be produced at a lower cost. Furthermore, by reducing the power required to operate the air separation device, it is possible to achieve so-called energy saving, so in today's world where there is a strong demand for energy saving, the industry plays a major role in this aspect.
第１図は従来の酸素製造方法を示す系統図、第
２図及び第３図は本発明に係る酸素製造方法を例
示する系統図である。
６……切換式熱交換器、８ａ……精留塔上塔、
８ｂ……精留塔下塔、１７……膨張タービン、１
７ａ……負荷ブロワ、３０……製品酸素圧送用圧
縮機、３１……蒸発器、３９……循環熱交換器、
４２……アフタクーラ。
FIG. 1 is a system diagram showing a conventional oxygen production method, and FIGS. 2 and 3 are system diagrams illustrating the oxygen production method according to the present invention. 6... Switching type heat exchanger, 8a... Rectification column upper column,
8b... Fractionation column lower column, 17... Expansion turbine, 1
7a... Load blower, 30... Compressor for pressure-feeding product oxygen, 31... Evaporator, 39... Circulating heat exchanger,
42...Aftercooler.
Claims (1)
て冷却した原料空気を精留塔下塔に導入して富酸
素液体空気と酸窒素液に粗精留した後、更にこれ
らの富酸素液体空気と富窒素液を精留塔上塔に導
入して高純度酸素成分、高純度窒素成分及び不純
窒素成分に夫々分離精製すると共に夫々を精留塔
上塔底部、同頂部及び同上部から抽気した後、上
記主熱交換器に送つて原料空気と熱交換すること
により温度回復を受けた後製品として取出す一
方、塔内を上昇する気体空気の一部を精留塔下塔
から抜出して上記主熱交換器の再熱回路を通過せ
しめた後膨張タービンに導入し、又膨張せしめ、
外部仕事を行なうことによつて系の熱平衡を成立
させる様にした空気分離方法において、前記精留
塔の外部に配置された蒸発器に精留塔上塔底部か
ら抜出された高純度液体酸素成分を液状で導入す
る一方、前記精留塔下塔から抜出された気体空気
の一部を循環熱交換器に通して昇温した後、前記
膨張タービンの負荷ブロワにかけて昇圧し、更に
該昇圧空気を前記循環熱交換器に通して冷却した
後、前記蒸発器内に設置されたリボイラに導入し
て高純度液体酸素成分を気化せしめると共に自ら
は液化し、気化酸素成分は上記主熱交換器に送る
一方、液化空気は前記精留塔下塔内に戻すことを
特徴とする空気分離方法。1. The feed air, which has been cooled by heat exchange with the low-temperature return gas in the main heat exchanger, is introduced into the lower column of the rectification column and crudely rectified into oxygen-enriched liquid air and oxynitrogen liquid. Air and nitrogen-rich liquid are introduced into the upper column of the rectification column, where they are separated and purified into high-purity oxygen components, high-purity nitrogen components, and impure nitrogen components, and each is extracted from the bottom, top, and upper part of the upper column of the rectification column. After that, it is sent to the main heat exchanger where it undergoes temperature recovery by exchanging heat with the feed air and is then taken out as a product.At the same time, a part of the gaseous air rising inside the column is extracted from the lower column of the rectification column and sent to the main heat exchanger. After passing through the reheat circuit of the heat exchanger, it is introduced into an expansion turbine and expanded again.
In an air separation method that establishes thermal equilibrium in the system by performing external work, high-purity liquid oxygen extracted from the top and bottom of the rectification column is sent to an evaporator placed outside the rectification column. While the components are introduced in liquid form, a part of the gaseous air extracted from the lower column of the rectification column is passed through a circulation heat exchanger to raise its temperature, and then the pressure is increased by the load blower of the expansion turbine, and the pressurized air is After being cooled through the circulation heat exchanger, it is introduced into a reboiler installed in the evaporator to vaporize the high-purity liquid oxygen component and liquefy itself, and the vaporized oxygen component is transferred to the main heat exchanger. An air separation method characterized in that while the liquefied air is sent, the liquefied air is returned to the lower column of the rectification column.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16807183A JPS6060484A (en) | 1983-09-12 | 1983-09-12 | Method of separating air |
| BR8403589A BR8403589A (en) | 1983-07-18 | 1984-07-18 | AIR SEPARATION PROCESS |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16807183A JPS6060484A (en) | 1983-09-12 | 1983-09-12 | Method of separating air |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6060484A JPS6060484A (en) | 1985-04-08 |
| JPH0323831B2 true JPH0323831B2 (en) | 1991-03-29 |
Family
ID=15861296
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP16807183A Granted JPS6060484A (en) | 1983-07-18 | 1983-09-12 | Method of separating air |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6060484A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0814459B2 (en) * | 1987-01-27 | 1996-02-14 | 日本酸素株式会社 | Air liquefaction separation method |
-
1983
- 1983-09-12 JP JP16807183A patent/JPS6060484A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6060484A (en) | 1985-04-08 |
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