JPS6138391B2 - - Google Patents
Info
- Publication number
- JPS6138391B2 JPS6138391B2 JP53110774A JP11077478A JPS6138391B2 JP S6138391 B2 JPS6138391 B2 JP S6138391B2 JP 53110774 A JP53110774 A JP 53110774A JP 11077478 A JP11077478 A JP 11077478A JP S6138391 B2 JPS6138391 B2 JP S6138391B2
- Authority
- JP
- Japan
- Prior art keywords
- column
- oxygen
- air
- heat exchanger
- rectification
- 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 46
- 239000001301 oxygen Substances 0.000 claims description 46
- 229910052760 oxygen Inorganic materials 0.000 claims description 46
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 42
- 229910052757 nitrogen Inorganic materials 0.000 claims description 19
- 238000007791 dehumidification Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 7
- 239000002699 waste material Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- 230000008929 regeneration Effects 0.000 claims description 6
- 238000011069 regeneration method Methods 0.000 claims description 6
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 4
- 239000007788 liquid Substances 0.000 description 11
- 239000002994 raw material Substances 0.000 description 10
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 6
- 238000010992 reflux Methods 0.000 description 4
- 229910052786 argon Inorganic materials 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000004804 winding Methods 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000010457 zeolite 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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed 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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
-
- 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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
-
- 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
- F25J3/04309—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 nitrogen
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
【発明の詳細な説明】
本発明は、大気から取入れた原料空気を圧縮、
脱湿、冷却および精留分離して、酸素、窒素等の
分離生成物を採取する空気分離方法に関するもの
で、製鉄所の高炉富化酸素、重質油および石炭の
ガス化炉の富化酸素等約90％の低純度の酸素を採
取する場合に適用されるものである。DETAILED DESCRIPTION OF THE INVENTION The present invention compresses raw air taken from the atmosphere.
This relates to an air separation method that collects separated products such as oxygen and nitrogen through dehumidification, cooling, and rectification. This is applied when collecting oxygen with a low purity of approximately 90%.
従来技術による酸素の採取方法を第１図に示
す。大気から取入れた原料空気を原料空気圧縮機
１で約５Kg/cm2Gに圧縮し、アフタークーラー２
で冷却した後空気熱交換器３で脱湿および冷却を
行ない、精留塔の下塔５で粗精留を行ない、精留
塔の上塔６でさらに精留を行なつて、製品酸素お
よび廃窒素に分離する。 A conventional method for collecting oxygen is shown in FIG. Raw air taken in from the atmosphere is compressed to approximately 5 kg/cm 2 G by raw air compressor 1, and then compressed to approximately 5 kg/cm2 G by air compressor 1.
After cooling in the air heat exchanger 3, dehumidification and cooling are carried out in the air heat exchanger 3, crude rectification is carried out in the lower column 5 of the rectification column, and further rectification is carried out in the upper column 6 of the rectification column to obtain product oxygen and Separate into waste nitrogen.
下塔５上部より抜出された窒素ガスは、空気熱
交換器３の再熱窒素として加熱された後空気熱交
換器３の中部より抜出されて膨脹タービン８で膨
脹し、精留塔の上塔６の上部より抜出され液体空
気および原料空気と熱交換して加熱された廃窒素
と合流して空気熱交換器３で温度回復して大気に
放出される。 Nitrogen gas extracted from the upper part of the lower column 5 is heated as reheated nitrogen in the air heat exchanger 3, then extracted from the middle of the air heat exchanger 3, expanded in the expansion turbine 8, and sent to the rectification column. It is extracted from the upper part of the upper column 6, joins with waste nitrogen that has been heated by exchanging heat with liquid air and raw material air, and is then temperature-recovered in the air heat exchanger 3 and released into the atmosphere.
精留塔の上塔６の下部より抜出された酸素は、
空気熱交換器３の巻込管を通つて温度回復し製品
酸素として採取される。 The oxygen extracted from the lower part of the upper column 6 of the rectification column is
The temperature is recovered through the winding pipe of the air heat exchanger 3, and the oxygen is collected as product oxygen.
約99.6％の高純度の酸素を採取する空気分離方
法においては、製品酸素の残り成分はほとんどア
ルゴンであるため、精留塔の上塔６の下部におけ
る酸素とアルゴンの分離が重要である。そのため
には、精留塔の下塔５に多量の原料空気を送入
し、主凝縮器７における蒸発量を多くし、精留塔
の上塔６下部の環流液量および上昇ガス量を多く
して、精留塔の上塔６の下部における精留を容易
にする必要がある。 In an air separation method that extracts oxygen with a high purity of approximately 99.6%, the remaining component of the product oxygen is almost entirely argon, so it is important to separate oxygen and argon in the lower part of the upper column 6 of the rectification column. To do this, a large amount of raw air is fed into the lower column 5 of the rectification column, the amount of evaporation in the main condenser 7 is increased, and the amount of reflux liquid and rising gas at the bottom of the upper column 6 of the rectification column is increased. Therefore, it is necessary to facilitate rectification in the lower part of the upper column 6 of the rectification column.
製品酸素純度が約97％以下になると、製品酸素
の残り成分はアルゴンの他に窒素も入るようにな
り、精留塔の上塔６の下部における精留は容易と
なつて、原料空気に含まれる酸素の約96％を製品
酸素として回収することができる。 When the product oxygen purity becomes approximately 97% or less, the remaining components of the product oxygen include nitrogen as well as argon, and rectification in the lower part of the upper column 6 of the rectification column becomes easy, and the remaining components of the product oxygen are reduced to less than 97%. Approximately 96% of the oxygen produced can be recovered as product oxygen.
従来技術による酸素の採取方法では、低純度の
酸素を採取する場合にも、１台の原料空気圧縮機
で所要原料空気の全量を約５Kg/cm2Gに圧縮し、
精留塔に送入していたため、原料空気圧縮機の消
費動力が大きい。 In the conventional oxygen collection method, even when collecting low-purity oxygen, one raw material air compressor compresses the total amount of raw material air to approximately 5 kg/cm 2 G.
Since the raw material air was sent to the rectification column, the power consumption of the raw air compressor was large.
本発明の目的は、低純度の酸素を採取する空気
分離方法において、消費動力を小さくすることに
ある。 An object of the present invention is to reduce power consumption in an air separation method for collecting low-purity oxygen.
本発明の要点は、原料空気を、吐出圧約５Kg/
cm2Ｇと吐出圧約0.5Kg/cm2Gの２台の原料空気圧縮
機で圧縮し、精留塔に送入することにある。 The key point of the present invention is that the raw material air has a discharge pressure of approximately 5 kg/
The raw material is compressed by two air compressors with a discharge pressure of approximately 0.5 kg/cm 2 G and a discharge pressure of approximately 0.5 Kg/cm 2 G, and then sent to the rectification column.
例えば、原料空気のうち約75％は約５Kg/cm2G
に圧縮され、アフタークーラーおよび空気熱交換
器を通つて精留塔の下塔に送入され、一部は膨脹
タービンで寒冷発生として使用されるが、他の一
部は主凝縮器において凝縮され、精留塔の上塔の
環流液および上昇ガスを生成して、精留が行なわ
れる。所要原料空気量の残りの約25％は約0.5Kg/
cm2Ｇに圧縮され、アフタークーラー、空気冷却
器、脱湿塔および酸素熱交換器を通つて精留塔の
上塔の中部にガス状態で送入される。 For example, about 75% of the raw air is about 5Kg/cm 2 G
It is compressed into a fraction and sent to the lower column of the rectification column through an aftercooler and an air heat exchanger, and a portion is used as cold generation in the expansion turbine, while the other portion is condensed in the main condenser. , the rectification is performed by producing a reflux liquid and a rising gas in the upper column of the rectification column. The remaining 25% of the required raw material air amount is approximately 0.5Kg/
It is compressed to cm 2 G and sent in a gaseous state to the middle part of the upper column of the rectification column through an aftercooler, an air cooler, a dehumidification tower and an oxygen heat exchanger.
製品酸素が低純度である場合には、精留塔の上
塔における精留が容易であり、原料空気を上塔の
中部にガス状態で送入しても、酸素を回収するこ
とができる。 When the product oxygen has low purity, rectification in the upper column of the rectification column is easy, and oxygen can be recovered even if raw air is fed in a gaseous state to the middle of the upper column.
以下、本発明の実施例を第２図によつて説明す
る。大気から取入れた原料空気は原料空気圧縮機
１で約５Kg/cm2Gに圧縮され、アフタークーラー
２で冷却水と熱交換して約40℃に冷却され、切替
使用される空気熱交換器３で廃窒素と熱交換して
約−170℃に冷却された後２分され、その一部は
直接精留塔の下塔５に送入され、他の一部は液化
器１０で廃窒素と熱交換して液化されて精留塔の
下塔５に送入される。 Embodiments of the present invention will be described below with reference to FIG. The raw air taken in from the atmosphere is compressed to approximately 5 kg/cm 2 G by the raw air compressor 1, and is cooled to approximately 40°C by exchanging heat with cooling water in the aftercooler 2, and then transferred to the air heat exchanger 3, which is switched and used. After exchanging heat with waste nitrogen and cooling it to approximately -170°C, it is divided into two parts, a part of which is directly sent to the lower column 5 of the rectification tower, and the other part is converted into waste nitrogen in the liquefier 10. It is liquefied by heat exchange and sent to the lower column 5 of the rectification column.
精留塔の下塔５では原料空気が粗精留され、上
部から窒素ガスおよび液体窒素が抜出され、下部
から液体空気が抜出される。下塔５上部から抜出
された窒素ガスは、酸素熱交換器１７の再熱窒素
として約−140℃まで加熱され酸素熱交換器１７
の中部ら抜出され、膨脹タービン８で約4.5Kg/cm2
Ｇから約0.3Kg/cm2Gに膨脹された後２分され、そ
の一部は液化器１０出口の廃ガスと合流して、空
気熱交換器３で常温まで温度回復し大気に放出さ
れ、他の一部は酸素熱交換器１７で常温まで温度
回復した後再生加熱器１８で加熱されて、脱湿塔
１６の再生に使用される。 In the lower column 5 of the rectification column, raw air is crudely rectified, nitrogen gas and liquid nitrogen are extracted from the upper part, and liquid air is extracted from the lower part. The nitrogen gas extracted from the upper part of the lower column 5 is heated to approximately -140°C as reheated nitrogen in the oxygen heat exchanger 17.
The middle part of the tube is extracted and the expansion turbine 8 generates approximately 4.5Kg/ cm2.
After being expanded from G to about 0.3Kg/cm 2 G, it is divided into two parts, a part of which joins the waste gas at the outlet of the liquefier 10, recovers the temperature to room temperature in the air heat exchanger 3, and is released into the atmosphere. The other part is recovered to room temperature in the oxygen heat exchanger 17, heated in the regeneration heater 18, and used for regeneration of the dehumidification tower 16.
下塔５上部から抜出された液体窒素は、精留塔
の上塔６の上部に環流液として送入され、下塔５
下部から抜出された液体空気は、炭化水素吸着器
１１を通つて炭化水素を除去された後、液体空気
過冷却器９で熱交換して過冷却され、上塔６の中
部に環流液として送入される。 The liquid nitrogen extracted from the upper part of the lower column 5 is sent to the upper part of the upper column 6 of the rectification column as a reflux liquid, and is then transferred to the upper column of the lower column 5.
The liquid air extracted from the lower part passes through the hydrocarbon adsorber 11 to remove hydrocarbons, is then supercooled by heat exchange in the liquid air supercooler 9, and is sent to the middle of the upper tower 6 as a reflux liquid. sent.
一方、大気から取入れた原料空気を低圧の原料
空気圧縮機１３により約0.5Kg/cm2Gに圧縮し、ア
フタークーラー１４で冷却水と熱交換して約40℃
に冷却し、更に空気冷却器１５で低温の冷媒と熱
交換して約５℃に冷却した後切替使用される脱湿
塔１６の合成ゼオライトで脱湿する。 On the other hand, raw air taken in from the atmosphere is compressed to approximately 0.5 kg/cm 2 G by a low-pressure raw air compressor 13, and heat exchanged with cooling water in an aftercooler 14 to approximately 40°C.
After cooling to about 5° C. by exchanging heat with a low-temperature refrigerant in an air cooler 15, it is dehumidified using synthetic zeolite in a dehumidification tower 16 which is switched to use.
脱湿した原料空気は、酸素熱交換器１７で製品
酸素、再熱窒素および脱湿塔１６再生用窒素と熱
交換して、精留塔の上塔６の中部に吹込まれる。 The dehumidified feed air exchanges heat with product oxygen, reheated nitrogen, and regenerating nitrogen of the dehumidification tower 16 in the oxygen heat exchanger 17, and is blown into the middle of the upper tower 6 of the rectification tower.
主凝縮器７で蒸発した酸素ガスの一部は上塔６
下部から抜出され、酸素熱交換器１７で常温まで
温度回復して製品酸素として採取される。 A part of the oxygen gas evaporated in the main condenser 7 is transferred to the upper tower 6.
The oxygen is extracted from the lower part, the temperature is recovered to room temperature in the oxygen heat exchanger 17, and the oxygen is collected as product oxygen.
本発明は以上述べたようにしたものであるか
ら、つぎのような効果がある。 Since the present invention is as described above, it has the following effects.
(1) 例えば所要原料空気量のうち約25％は吐出圧
約0.5Kg/cm2Gでよいので、原料空気圧縮機の消
費動力が小さくなり、製品酸素あたりの消費動
力は従来の低純度酸素を採取する空気分離装置
に比較して約80％になる。(1) For example, about 25% of the required amount of raw material air can be supplied at a discharge pressure of about 0.5Kg/cm 2 G, so the power consumption of the raw material air compressor is reduced, and the power consumption per product oxygen is lower than that of conventional low-purity oxygen. This is approximately 80% compared to the air separation equipment that collects the air.
(2) 製品酸素、再熱窒素およびゲル塔再生用窒素
は酸素熱交換器で熱交換させるので、空気熱交
換器の巻込管が不要になり、設備費が低減す
る。(2) Product oxygen, reheated nitrogen, and gel tower regeneration nitrogen are heat exchanged in an oxygen heat exchanger, eliminating the need for an air heat exchanger winding tube and reducing equipment costs.
第１図は従来技術による酸素の採取法を示した
空気分離装置の系統図、第２図は本発明による低
純度の酸素を採取する方法を実施した空気分離装
置の一例を示す系統図である。
１，１３……原料空気圧縮機、２，１４……ア
フタークーラー、３……空気熱交換器、４……逆
止弁、５……精留塔下塔、６……精留塔上塔、７
……主凝縮器、８……膨脹タービン、９……液体
空気過冷却器、１０……液化器、１１……炭化水
素吸着器、１２……循環吸着器、１５……空気冷
却器、１６……脱湿塔、１７……酸素熱交換器、
１８……再生加熱器。
FIG. 1 is a system diagram of an air separation device showing a method of collecting oxygen according to the prior art, and FIG. 2 is a system diagram showing an example of an air separation device implementing a method of collecting low-purity oxygen according to the present invention. . 1, 13... Raw material air compressor, 2, 14... Aftercooler, 3... Air heat exchanger, 4... Check valve, 5... Lower column of rectification column, 6... Upper column of rectification column, 7
... Main condenser, 8 ... Expansion turbine, 9 ... Liquid air supercooler, 10 ... Liquefier, 11 ... Hydrocarbon adsorption device, 12 ... Circulating adsorption device, 15 ... Air cooler, 16 ... Dehumidification tower, 17 ... Oxygen heat exchanger,
18...Regeneration heater.
Claims (1)
た後精留塔の下塔に導入して粗精留を行ない、更
に精留塔の上塔で精留を行なつて製品酸素および
廃窒素に分離する深冷式空気分離方法において、
酸素を採取するために必要な原料空気を下塔と上
塔に供給する空気量に分け、下塔に供給する空気
量を約５Kg/cm2Gに圧縮し空気熱交換器で脱湿冷
却した後精留塔の下塔に導入し、上塔に供給する
空気量を約0.5Kg/cm2Gに圧縮し脱湿塔で脱湿し、
酸素熱交換器で製品酸素、再熱窒素および脱湿塔
再生用廃窒素と熱交換して冷却した後精留塔の上
塔中部に導入し、前記精留塔の下塔で精留分離さ
れた窒素ガスの一部を前記酸素熱交換器に導入し
て加熱し、膨張タービンで膨張させた後２分し、
その一部を精留塔の上塔頂部より抜出された廃窒
素と合流させ、空気熱交換器で温度回復させて大
気に放出し、他の一部を酸素熱交換器で温度回復
させて前記脱湿塔の再生に利用し、精留塔の上塔
下部より抜出された酸素を酸素熱交換器で温度回
復させ、製品酸素として採取するようにしたこと
を特徴とする低純度の酸素を採取する方法。1 After compressing the raw air and dehumidifying and cooling it with an air heat exchanger, it is introduced into the lower column of the rectification column for crude rectification, and further rectified in the upper column of the rectification column to produce oxygen product and waste. In the cryogenic air separation method that separates into nitrogen,
The raw air necessary for extracting oxygen was divided into the amount of air supplied to the lower tower and the upper tower, and the amount of air supplied to the lower tower was compressed to approximately 5 kg/cm 2 G and dehumidified and cooled with an air heat exchanger. The air is introduced into the lower column of the post-rectification column, and the amount of air supplied to the upper column is compressed to approximately 0.5Kg/cm 2 G, and then dehumidified in the dehumidification column.
After being cooled by heat exchange with the product oxygen, reheated nitrogen, and waste nitrogen for dehumidification tower regeneration in an oxygen heat exchanger, it is introduced into the middle of the upper column of the rectification column, and is then rectified and separated in the lower column of the rectification column. A part of the nitrogen gas is introduced into the oxygen heat exchanger, heated, and expanded in an expansion turbine for 2 minutes,
A part of the nitrogen is combined with the waste nitrogen extracted from the top of the rectification tower, and the temperature is recovered in an air heat exchanger and then released into the atmosphere.The other part is recovered in temperature in an oxygen heat exchanger. Low-purity oxygen, which is used for regeneration of the dehumidification tower, and is characterized in that the oxygen extracted from the lower part of the upper column of the rectification tower is temperature-recovered in an oxygen heat exchanger and collected as product oxygen. How to collect.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11077478A JPS5538423A (en) | 1978-09-11 | 1978-09-11 | Method of extracting low purity oxygen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11077478A JPS5538423A (en) | 1978-09-11 | 1978-09-11 | Method of extracting low purity oxygen |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5538423A JPS5538423A (en) | 1980-03-17 |
| JPS6138391B2 true JPS6138391B2 (en) | 1986-08-29 |
Family
ID=14544245
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11077478A Granted JPS5538423A (en) | 1978-09-11 | 1978-09-11 | Method of extracting low purity oxygen |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5538423A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60221681A (en) * | 1985-03-27 | 1985-11-06 | 株式会社日立製作所 | Air separation equipment raw air cooling temperature control device |
| FR3110685B1 (en) * | 2020-05-20 | 2022-12-23 | Air Liquide | Process and apparatus for air separation by cryogenic distillation |
| EP4425078A1 (en) * | 2023-03-02 | 2024-09-04 | Linde GmbH | Process and apparatus for purifying air and cryogenic air separation process and plant |
-
1978
- 1978-09-11 JP JP11077478A patent/JPS5538423A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5538423A (en) | 1980-03-17 |
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