JPH02275282A - Air liquefaction separation method - Google Patents
Air liquefaction separation methodInfo
- Publication number
- JPH02275282A JPH02275282A JP1096813A JP9681389A JPH02275282A JP H02275282 A JPH02275282 A JP H02275282A JP 1096813 A JP1096813 A JP 1096813A JP 9681389 A JP9681389 A JP 9681389A JP H02275282 A JPH02275282 A JP H02275282A
- Authority
- JP
- Japan
- Prior art keywords
- air
- booster
- product
- heat exchanger
- expansion turbine
- 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.)
- Granted
Links
- 238000000926 separation method Methods 0.000 title claims description 14
- 239000000047 product Substances 0.000 claims description 34
- 239000002994 raw material Substances 0.000 claims description 23
- 239000012263 liquid product Substances 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 4
- 238000000034 method Methods 0.000 claims description 4
- 239000012535 impurity Substances 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 claims description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 15
- 239000001301 oxygen Substances 0.000 abstract description 15
- 229910052760 oxygen Inorganic materials 0.000 abstract description 15
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 abstract description 13
- 229910001882 dioxygen Inorganic materials 0.000 abstract description 11
- 238000005070 sampling Methods 0.000 abstract description 5
- 239000002131 composite material Substances 0.000 abstract 3
- 238000005057 refrigeration Methods 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 7
- 239000007789 gas Substances 0.000 description 7
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 229910001873 dinitrogen Inorganic materials 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
- F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、空気波化分離方法に関し、特にガス状製品と
液状製品とを併産するのに適した空気波化分離方法に関
する。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to an air wave separation method, and particularly to an air wave separation method suitable for co-producing gaseous products and liquid products.
原料空気を圧縮、精製した後に液化点付近まで冷却し、
精留塔に導入して液化精留分離し、窒素や酸素等を得る
空気波化分離方法が知られている。After compressing and refining raw air, it is cooled to near the liquefaction point.
An air wave separation method is known in which air is introduced into a rectification column and subjected to liquefaction rectification separation to obtain nitrogen, oxygen, and the like.
この空気波化分離方法で液状の製品、例えば液化酸素を
得る場合には、プロセス成立上の必要寒冷を供給するた
めに系内に膨脹タービンを配している。When a liquid product, such as liquefied oxygen, is obtained by this air wave separation method, an expansion turbine is disposed within the system to supply the necessary refrigeration to establish the process.
第２図は、ガス状の酸素（酸素ガス）と液状の酸素（液
化酸素）とを併産する従来の空気波化分離方法の一例を
示すもので、上記膨脹タービンを原料空気導入系に設け
たものである。Figure 2 shows an example of a conventional air wave separation method that co-produces gaseous oxygen (oxygen gas) and liquid oxygen (liquefied oxygen). It is something that
原料空気圧縮機１て圧縮された原料空気Ａは、冷却器２
で常温に冷却され、切替え使用される吸着器３．３の一
方で水分や炭酸ガス等の不純物を除去された後に、主熱
交換器４に導入される。この原料空気Ａの大部分は、該
主熱交換器４で後述の製品酸素ガスＧＯや排ガスＷによ
り液化点付近まで冷却された後に減圧弁５で下部塔圧力
に減圧されて複精留塔６の下部塔７に導入される。原料
空気Ａの一部Ａｔは、中間温度まで冷却された状態で主
熱交換器４の中部から導出され、膨脹タービン８に導入
されて下部塔圧力まで膨脹し、寒冷を発生して前記下部
塔７に導入される大部分の原料空気Ａと略同じ温度に降
温した後に、原料空気Ａと合流して下部塔７に導入され
る。The raw air A compressed by the raw air compressor 1 is sent to the cooler 2.
After being cooled to room temperature and having impurities such as moisture and carbon dioxide removed by one of the adsorbers 3.3 which is switched to use, it is introduced into the main heat exchanger 4. Most of this raw air A is cooled to near the liquefaction point by the product oxygen gas GO and exhaust gas W, which will be described later, in the main heat exchanger 4, and then is reduced in pressure to the lower column pressure in the pressure reducing valve 5, and then transferred to the double rectification column 6. is introduced into the lower column 7. A part of the feed air A is led out from the middle part of the main heat exchanger 4 in a state where it has been cooled to an intermediate temperature, is introduced into the expansion turbine 8, is expanded to the pressure of the lower column, generates refrigeration, and is discharged from the lower column. After cooling down to approximately the same temperature as most of the raw material air A introduced into the lower column 7, it is combined with the raw material air A and introduced into the lower column 7.
下部塔７に導入された原料空気Ａは、請合分離されて下
部塔７下部の液化空気ＬＡと下部塔７上部の窒素ガスＧ
Ｎとに分離する。下部塔７下部の液化空気ＬＡは、下部
塔７底部から導出され、適冷器９を経て上部塔１０の中
部に導入される。また下部塔７上部の窒素ガスＧＮは、
主凝縮蒸発器１１で凝縮液化され、下部塔７の還流液に
なるとともに、その一部が適冷器９を経て上部塔１０の
上部に導入される。The feed air A introduced into the lower column 7 is separated into liquefied air LA at the bottom of the lower column 7 and nitrogen gas G at the upper part of the lower column 7.
Separate into N. The liquefied air LA at the bottom of the lower column 7 is led out from the bottom of the lower column 7 and introduced into the middle of the upper column 10 through the appropriate cooler 9. In addition, the nitrogen gas GN at the top of the lower column 7 is
It is condensed and liquefied in the main condensing evaporator 11 to become a reflux liquid in the lower column 7 , and a part of it is introduced into the upper part of the upper column 10 via the appropriate cooler 9 .
上部塔１０内での精留分離操作により、その底部に分離
した液化酸素ＬＯは、一部が導管１２を経て製品液化酸
素ＬＯとして採取され、残部が主凝縮蒸発器１１で蒸発
気化して上部塔１０の上昇ガスになるとともに、その一
部が製品酸素ガスＧＯとして導管１３から採取され、主
熱交換器４を経て導出される。また上部塔１０上部に分
離した窒素ガスＧＮは、頂部の導管１４から導出され、
適冷″ａ９．主熱交換器４を経て排ガスＷとして排出さ
れる。Due to the rectification separation operation in the upper column 10, part of the liquefied oxygen LO separated at the bottom is collected as a product liquefied oxygen LO through the conduit 12, and the remainder is evaporated in the main condenser evaporator 11 and sent to the upper part. It becomes the ascending gas of the column 10, and a part of it is collected from the conduit 13 as the product oxygen gas GO and led out via the main heat exchanger 4. Further, the nitrogen gas GN separated in the upper part of the upper column 10 is led out from the conduit 14 at the top,
Appropriate cooling "a9. It is discharged as exhaust gas W through the main heat exchanger 4.
通常、このような空気波化分離方法においては、製品酸
素ガスＧＯと製品液化酸素ＬＯの量に応じて膨脹タービ
ン８のガス流量、即ち寒冷発生量を設定し、略一定の割
合でガス状製品を液状製品とを得ており、ガス状製品と
液状製品との割合を変える場合には、膨脹タービン８に
導入する原料空気量を弁５等により調整して膨脹タービ
ン８における寒冷発生量を増減させていた。Normally, in such an air wave separation method, the gas flow rate of the expansion turbine 8, that is, the amount of refrigeration generated, is set according to the amount of the product oxygen gas GO and the product liquefied oxygen LO, and the gaseous product is produced at a substantially constant rate. is obtained as a liquid product, and when changing the ratio of gaseous product and liquid product, the amount of raw air introduced into the expansion turbine 8 is adjusted by the valve 5 etc. to increase or decrease the amount of cold generation in the expansion turbine 8. I was letting it happen.
しかしながら、上述のごとく原料空気導入系に膨脹ター
ビンを配したものでは、膨脹タービンに導入する原料空
気の圧力を原料空気圧縮機で得ているために１．゛膨張
タービンに導入しない分の原料空気も高い圧力に圧縮し
なければならず、原料空気圧縮機の動力消費量が多くな
り、得られる製品の動力原単位を悪化させていた。However, in the case where the expansion turbine is disposed in the raw material air introduction system as described above, the pressure of the raw material air introduced into the expansion turbine is obtained by the raw material air compressor. ``The raw air that is not introduced into the expansion turbine must also be compressed to a high pressure, which increases the power consumption of the raw air compressor and worsens the power consumption of the resulting product.
また、ガス状製品と液状製品との割合の調整幅にも限度
があり、大幅な需要変動には対処することができなかっ
た。Furthermore, there is a limit to the adjustment range of the ratio of gaseous products to liquid products, and it has not been possible to cope with large fluctuations in demand.
そこで、本発明は、製品の動力原単位を低減するととも
に、ガス状製品と液状製品との採取割合を容易に、かつ
大幅に調整することのできる空気波化分離方法を提供す
ることを目的としている。Therefore, the present invention aims to provide an air wave separation method that can reduce the power consumption of the product and easily and significantly adjust the sampling ratio of gaseous products and liquid products. There is.
上記した目的を達成するために本発明は、原料空気を圧
縮し、吸着によって不純物を除去した後、主熱交換器で
冷却し、複精留塔に導入して液化精留分離し、ガス状及
び／又は液状の製品を得る方法において、吸着器を導出
した原料空気を２分し、その一方を主熱交換器に導入し
て液化点付近まで、又は一部液化するまで冷却後、複精
留塔の下部塔に導入するとともに、他方をガス状製品採
取量及び液状製品採取量に応じて複数段もしくは複数基
からなる昇圧機の任意の数を選択して導入昇圧後、主熱
交換器に導入して中間温度まで冷却して導出し、膨脹タ
ービンに導入して降圧、膨脹させた後に複精留塔に導入
することを特徴とする空気波化分離方法を提供するもの
である。In order to achieve the above object, the present invention compresses raw air, removes impurities by adsorption, cools it in a main heat exchanger, introduces it into a double rectification column, liquefies it and rectifies it, and separates it into a gaseous state. And/or in a method for obtaining a liquid product, the raw air discharged from the adsorber is divided into two parts, one of which is introduced into the main heat exchanger and cooled to near the liquefaction point or until partially liquefied, and then subjected to double distillation. It is introduced into the lower column of the distillation column, and the other is introduced by selecting an arbitrary number of boosters consisting of multiple stages or multiple units depending on the amount of gaseous product collected and the amount of liquid product collected. After increasing the pressure, the main heat exchanger The present invention provides an air wave separation method characterized in that the air is introduced into the air, cooled to an intermediate temperature, extracted, introduced into an expansion turbine, reduced in pressure and expanded, and then introduced into a double rectification column.
上述のごとく、複数段もしくは複数基からなる昇圧機の
任意の数を選択して原料空気の一部を昇圧することによ
り、膨脹タービンに導入する原料ガス量及び圧力を容易
に、かつ大幅に変更することができ、膨脹タービンにお
ける寒冷量を大幅に増減させることができる。As mentioned above, the amount and pressure of the raw material gas introduced into the expansion turbine can be easily and significantly changed by increasing the pressure of a part of the raw material air by selecting any number of boosters consisting of multiple stages or multiple units. This allows the amount of refrigeration in the expansion turbine to be significantly increased or decreased.
以下、本発明を第１図に示す一実施例に基づいてさらに
詳細に説明する。尚、以下の説明において前記第２図に
示した従来例と同一要素のものには同一符号を付して詳
細な説明を省略する。Hereinafter, the present invention will be explained in more detail based on an embodiment shown in FIG. In the following description, the same elements as those in the conventional example shown in FIG.
原料空気圧縮機１で所定の圧力まで圧縮され、吸着器３
で精製された原料空気Ａは、吸着器３を導出した後に導
管２０．２１に２分される。一方の大部分の原料空気Ａ
ｍは、導管２０を経て主熱交換器４に導入され、製品酸
素ガスＧｏ及び排ガスＷにより液化点付近まで、又は一
部液化されるまで冷却されて複精留塔６の下部塔７に導
入される。The raw material air is compressed to a predetermined pressure by the compressor 1, and then transferred to the adsorber 3.
The purified raw material air A is divided into two pipes 20 and 21 after being led out of the adsorber 3. On the other hand, most of the raw material air A
m is introduced into the main heat exchanger 4 via the conduit 20, cooled by the product oxygen gas Go and exhaust gas W to near the liquefaction point or until partially liquefied, and introduced into the lower column 7 of the double rectification column 6. be done.
他方の一部の原料空気Ａｔは、導管２１を経て第−昇圧
機２２．第二昇圧機２３．及び第三昇圧機２４を直列に
備えた昇圧回路２５に導入される。The other part of the raw air At passes through the conduit 21 to the second booster 22. Second booster 23. and is introduced into a booster circuit 25 including a third booster 24 in series.
これらの各昇圧機２２，２３．２４には、その二次側に
それぞれアフタークーラー２２ ａ、 ２３ ａ。Each of these boosters 22, 23, 24 has an aftercooler 22a, 23a on its secondary side, respectively.
２４ａが配設されており、さらに第−昇圧機２２及び第
二昇圧機２３のアフタークーラー２２ａ。24a is provided, and furthermore, an aftercooler 22a of the first booster 22 and the second booster 23.
２３Ｈの導出側には弁２２ｂ、２３ｂを有するバイパス
管２２ｃ、２３ｃが接続されている。Bypass pipes 22c and 23c having valves 22b and 23b are connected to the outlet side of 23H.
この昇圧回路２５は、ガス状製品（酸素ガスＧＯ）採取
量及び液状製品（液化酸素ＬＯ）採取量に応じて制御さ
れるもので、例えば、製品酸素ガスＧｏを多く採取する
場合には、第二昇圧機２３に付属する弁２３ｂを開き、
第−昇圧機２２に付属する弁２２ｂを閉じて第三昇圧機
２４のみを作動させて原料空気Ａｔを昇圧して主熱交換
器４に導入し、中間温度まで冷却して膨脹タービン８に
導入する。This booster circuit 25 is controlled according to the amount of gaseous product (oxygen gas GO) and liquid product (liquefied oxygen LO) collected. For example, when collecting a large amount of product oxygen gas Go, Open the valve 23b attached to the second booster 23,
The valve 22b attached to the first booster 22 is closed and only the third booster 24 is operated to boost the pressure of the feed air At, introduce it into the main heat exchanger 4, cool it to an intermediate temperature, and introduce it into the expansion turbine 8. do.
また、寒冷量を多く必要とする製品液化酸素ＬＯを多く
採取する場合には、全昇圧機２２，２３゜２４を作動さ
せるとともに、第−昇圧機２２及び第二昇圧機２３に付
属する弁２２ｂ、２３ｂを閉じて原料空気Ａｔを三段階
に圧縮して高圧とし、導管２４ｃから主熱交換器４に導
入し、中間温度まで冷却して膨脹タービン８に導入する
。In addition, when collecting a large amount of product liquefied oxygen LO that requires a large amount of refrigeration, all boosters 22, 23 and 24 are operated, and the valve 22b attached to the first booster 22 and second booster 23 is activated. , 23b are closed, and the raw air At is compressed in three stages to a high pressure, introduced into the main heat exchanger 4 through the conduit 24c, cooled to an intermediate temperature, and introduced into the expansion turbine 8.
さらに第二昇圧機２３及び第三昇圧機２４を作動させて
第−昇圧機２２を不作動とすれば、膨脹タービン８に導
入する原料空気Ａｔの圧力を上記両圧力の中間圧力とす
ることができる。Further, by activating the second booster 23 and the third booster 24 and disabling the second booster 22, the pressure of the raw material air At introduced into the expansion turbine 8 can be set to an intermediate pressure between the above two pressures. can.
次表は、本実施例における運転モードを示すもので、製
品液化酸素ＬＯを大量に得るための液製品採取モード、
製品液化酸素ＬＯを少量として製品酸素ガスＧＯを主に
得るガス製品採取モード、及びその中間のモードにおけ
る各部の原料空気（Ａ、Ａｍ、Ａｔ）の流量と圧力、及
び採取される製品（ＬＯ，Ｇｏ）Ｍｋを示すものである
。The following table shows the operation modes in this example: a liquid product collection mode to obtain a large amount of product liquefied oxygen LO;
The flow rate and pressure of the raw material air (A, Am, At) at each part in the gas product sampling mode where the product oxygen gas GO is mainly obtained with a small amount of the product liquefied oxygen LO, and the mode in between, and the sampled product (LO, Go) Mk.
このように、製品酸素ガスＧｏの採取量及び製品液化酸
素ＬＯの採取量に応じて、昇圧機の数を選択して原料空
気Ａｔを昇圧することにより、膨脹タービン８に導入す
る原料空気Ａｔの圧力、即ちその量を変えることができ
、操作条件に合った寒冷量を得ることができる。In this way, by selecting the number of boosters and boosting the pressure of the feed air At depending on the amount of product oxygen gas Go and the amount of product liquefied oxygen LO, the amount of feed air At introduced into the expansion turbine 8 can be increased. The pressure, and thus the amount, can be varied to obtain the amount of refrigeration that suits the operating conditions.
また、膨脹タービン８に導入する原料空気Ａｔに必要な
圧力を昇圧機で得ているので、原料空気圧縮ａｌｌにお
ける原料空気への圧縮圧力を下部塔７の精留操作に必要
な圧力にすることができるから、原料空気Ａの全てを膨
脹タービン８に必要な圧力まで圧縮する必要がなくなり
、原料空気圧縮機１の所要動力を大幅に低減す、ること
かできる。In addition, since the pressure necessary for the feed air At introduced into the expansion turbine 8 is obtained by the booster, the compression pressure for the feed air in the feed air compression all can be set to the pressure necessary for the rectification operation of the lower column 7. Therefore, there is no need to compress all of the raw material air A to the pressure required for the expansion turbine 8, and the power required for the raw material air compressor 1 can be significantly reduced.
このとき、前記昇圧回路２５においては、全原料空気Ａ
を分岐した一部の原料空気Ａｔを昇圧するだけであるか
ら、流量が少ないことに加えて圧縮率が小さいので、そ
の所要動力も僅かであり、上記原料空気圧縮機１の大幅
な動力費低減により、得られる製品の動力原単位を低減
することができる。At this time, in the booster circuit 25, all the raw material air A
Since only a part of the feed air At branched off is pressurized, the flow rate is small and the compression ratio is small, so the power required is small, and the power cost of the feed air compressor 1 is significantly reduced. As a result, the power consumption of the resulting product can be reduced.
特に、前記各昇圧機の内、常時作動状態に設定する昇圧
機、すなわち上記実施例に置いては第三昇圧機２４を膨
脹タービン制動ブロワ−１あるいは原料空気圧縮機１と
のコンバイン型とすることにより、該昇圧機の動力費を
不要としたり、あるいはごく僅かなものにすることがで
きる。In particular, among the boosters, the booster set to be in constant operation, that is, the third booster 24 in the above embodiment, is a combine type with the expansion turbine brake blower 1 or the raw air compressor 1. As a result, the power cost for the booster can be eliminated or reduced to a very small amount.
尚、上記実施例では、昇圧機を３台配置し、第三昇圧機
２４を常時作動の昇圧機とした例で説明したが、２台の
昇圧機でも十分な作用を発揮することができ、導管の配
置や昇圧機の種類により、常時作動の昇圧機を前段とす
ることも可能である。In the above embodiment, three boosters are arranged and the third booster 24 is a constantly operating booster, but even two boosters can provide sufficient effect. Depending on the arrangement of the conduits and the type of booster, it is also possible to use a constantly operating booster as the first stage.
さらに、多段式圧縮機を用いて、該多段式圧縮機の後段
あるいは前段を任意に切離したり、中…工部から中間圧
力の原料空気Ａｔを取出したりすることにより、上記実
施例同様に、膨脹タービン８に導入する原料空気Ａｔの
圧力及び流量の調節を行うことが可能である。Furthermore, by using a multi-stage compressor, by arbitrarily separating the rear stage or the front stage of the multi-stage compressor, or by taking out the raw material air At at an intermediate pressure from the central part, expansion can be carried out in the same way as in the above embodiment. It is possible to adjust the pressure and flow rate of the raw material air At introduced into the turbine 8.
また、本実施例に示すように、膨脹タービン８で膨脹し
た後の原料空気Ａｔを操作圧力の低い上部塔１０に導入
することにより、膨脹タービン８における原料空気Ａｔ
の膨張率を大きくとれ、寒冷量をより多くすることがで
きるが、従来と同様に下部塔７の操作圧力まで膨脹させ
て下部塔７に導入しても、必要な寒冷量を得ることは容
易である。Further, as shown in this embodiment, by introducing the raw material air At after being expanded in the expansion turbine 8 into the upper column 10 where the operating pressure is low, the raw material air At in the expansion turbine 8 is
Although it is possible to increase the expansion rate of , and to increase the amount of refrigeration, it is easy to obtain the necessary amount of refrigeration even if it is expanded to the operating pressure of the lower column 7 and introduced into the lower column 7 as in the past. It is.
さらに、本発明方法で得られる液状製品としては、上記
酸素の他、窒素やアルゴン等、従来から液状で採取され
ているもの全てを含むことができ、ガス状製品と液状製
品の種類の組合せは任意に選定することができる。Furthermore, in addition to the above-mentioned oxygen, the liquid product obtained by the method of the present invention can include all the substances conventionally collected in liquid form, such as nitrogen and argon. It can be selected arbitrarily.
以上説明したように、本発明は、原料空気の一部をガス
状製品採取量及び液状製品採取量に応じて複数段もしく
は複数基からなる昇圧機の任意の数を選択して昇圧後、
中間温度まで冷却して膨脹タービンに導入するから、製
品の採取状態により膨脹タービンの吸入側圧力、即ち吸
入量が変化し、操作状態に合った最適な寒冷量を得るこ
とができる。また複数の昇圧機を選択して昇圧するから
、膨脹タービンの吸入側圧力及び流量を大きく変えるこ
とができるので、膨脹タービンにおける発生寒冷量を大
幅に変化させることができ、ガス状製品と液状製品との
採取割合の大幅な増減が可能となる。さらに、原料空気
全量を膨脹タービンの吸入圧力に合せて圧縮する必要が
ないので、原料空気圧縮機の動力費を大幅に低減させる
ことができる。As explained above, in the present invention, after pressurizing a part of the raw air by selecting an arbitrary number of boosters consisting of multiple stages or multiple units depending on the amount of gaseous product and liquid product collected,
Since the product is cooled to an intermediate temperature and introduced into the expansion turbine, the pressure on the suction side of the expansion turbine, that is, the suction amount, changes depending on the state of product collection, making it possible to obtain the optimum amount of refrigeration that matches the operating conditions. In addition, since multiple boosters are selected to increase the pressure, the suction side pressure and flow rate of the expansion turbine can be greatly changed, so the amount of cooling generated in the expansion turbine can be greatly changed, and the pressure can be increased between gaseous products and liquid products. This makes it possible to significantly increase or decrease the sampling rate. Furthermore, since it is not necessary to compress the entire amount of feed air to match the suction pressure of the expansion turbine, the power cost of the feed air compressor can be significantly reduced.
特に、常時作動状態に設定する昇圧機を膨脹タービン制
動ブロワ−あるいは原料空気圧縮機とのコンバイン型と
することにより、該昇圧機の動力費を不要としたり、あ
るいはごく住かなものにできるので、採取する製品の動
力原単位をさらに低減することができる。In particular, by making the booster that is always in operation a combination type with an expansion turbine brake blower or a raw air compressor, the power cost of the booster can be eliminated or it can be made very inconvenient. The power consumption of the product to be collected can be further reduced.
第１図は本発明の一実施例を示す系統図、第２図は従来
例を示す系統図である。
１・・・原料空気圧縮機 ３・・・吸若器 ４・・
・主熱交換器 ６・・・複精留塔 ８・・・膨脹タ
ービン２２・・・第−昇圧機 ２３・・・第二昇圧機
２４・・・第三昇圧機 Ａ・・・原料空気 Ｇ
Ｏ・・・製品酸素ガス
ＬＯ・・・製品液化酸素
特
許
出
願
人
日
本
酸
素
株
式FIG. 1 is a system diagram showing one embodiment of the present invention, and FIG. 2 is a system diagram showing a conventional example. 1... Raw material air compressor 3... Young absorber 4...
・Main heat exchanger 6... Double rectifier 8... Expansion turbine 22... No. 1 booster 23... Second booster 24... Third booster A... Raw material air G
O... Product oxygen gas LO... Product liquefied oxygen Patent applicant Nippon Sanso Co., Ltd.
Claims (1)
後、主熱交換器で冷却し、複精留塔に導入して液化精留
分離し、ガス状及び／又は液状の製品を得る方法におい
て、吸着器を導出した原料空気を２分し、その一方を主
熱交換器に導入して液化点付近まで、又は一部液化する
まで冷却後、複精留塔の下部塔に導入するとともに、他
方をガス状製品採取量及び液状製品採取量に応じて複数
段もしくは複数基からなる昇圧機の任意の数を選択して
導入昇圧後、主熱交換器に導入して中間温度まで冷却し
て導出し、膨脹タービンに導入して降圧、膨脹させた後
に複精留塔に導入することを特徴とする空気液化分離方
法。 ２、前記複数基の昇圧機の内、任意の１基が膨脹タービ
ン制動ブロワーであることを特徴とする請求項１記載の
空気液化分離方法。 ３、前記複数基の昇圧機の内、任意数の昇圧機が原料空
気圧縮機とのコンバイン型であることを特徴とする請求
項１記載の空気波化分離方法。[Claims] 1. After compressing the raw material air and removing impurities by adsorption, it is cooled in a main heat exchanger, introduced into a double rectification column, and separated by liquefaction rectification to produce gaseous and/or liquid In the method of obtaining the product, the raw air discharged from the adsorber is divided into two parts, one of which is introduced into the main heat exchanger and cooled to near the liquefaction point or until partially liquefied. At the same time as introducing it into the column, the other one is introduced by selecting an arbitrary number of boosters consisting of multiple stages or multiple units depending on the amount of gaseous product collected and the amount of liquid product collected. After increasing the pressure, it is introduced into the main heat exchanger. An air liquefaction separation method characterized by cooling the air to an intermediate temperature, leading it out, introducing it into an expansion turbine, reducing the pressure and expanding it, and then introducing it into a double rectification column. 2. The air liquefaction separation method according to claim 1, wherein any one of the plurality of boosters is an expansion turbine brake blower. 3. The air wave separation method according to claim 1, wherein any number of the boosters among the plurality of boosters are of a combine type with a raw material air compressor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1096813A JP2736543B2 (en) | 1989-04-17 | 1989-04-17 | Air liquefaction separation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1096813A JP2736543B2 (en) | 1989-04-17 | 1989-04-17 | Air liquefaction separation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02275282A true JPH02275282A (en) | 1990-11-09 |
| JP2736543B2 JP2736543B2 (en) | 1998-04-02 |
Family
ID=14175035
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1096813A Expired - Fee Related JP2736543B2 (en) | 1989-04-17 | 1989-04-17 | Air liquefaction separation method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2736543B2 (en) |
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| JP2010536004A (en) * | 2007-08-10 | 2010-11-25 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Method and apparatus for separating air by cryogenic distillation |
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1989
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| JP2010536003A (en) * | 2007-08-10 | 2010-11-25 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Method and apparatus for separating air by cryogenic distillation |
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