JP2000258054A - Method and apparatus for manufacturing low purity oxygen - Google Patents
Method and apparatus for manufacturing low purity oxygenInfo
- Publication number
- JP2000258054A JP2000258054A JP11061574A JP6157499A JP2000258054A JP 2000258054 A JP2000258054 A JP 2000258054A JP 11061574 A JP11061574 A JP 11061574A JP 6157499 A JP6157499 A JP 6157499A JP 2000258054 A JP2000258054 A JP 2000258054A
- Authority
- JP
- Japan
- Prior art keywords
- oxygen
- fraction
- low
- liquid fraction
- pressure 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.)
- Granted
Links
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
- F25J3/0446—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 the heat generated by mixing two different phases
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
- F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
-
- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/52—Oxygen production with multiple purity O2
-
- 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
-
- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
-
- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/42—One fluid being 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
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)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、低純度酸素の製造
方法及び装置に関し、詳しくは、低温で空気を蒸留分離
して低純度酸素を製品として回収するプロセスであっ
て、圧縮機を使用することなく比較的高圧力の製品低純
度酸素を製造するための方法及び装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and apparatus for producing low-purity oxygen, and more particularly to a process for recovering low-purity oxygen as a product by distilling and separating air at a low temperature, using a compressor. The present invention relates to a method and an apparatus for producing a product low-purity oxygen at a relatively high pressure without the need.
【０００２】[0002]
【従来の技術及び発明が解決しようとする課題】低純度
酸素は、ガス化複合発電（ＩＧＣＣ）や、直接・溶融還
元製鋼及びガラス溶融等で使用される。これらのアプリ
ケーションでは、大量の酸素を消費することから、特に
動力原単位が低いことが要求される。BACKGROUND OF THE INVENTION Low-purity oxygen is used in integrated gasification combined cycle (IGCC), direct smelting reduction steelmaking and glass melting. These applications require a particularly low power consumption due to the large consumption of oxygen.
【０００３】Ｃａｍｂｅｒｌｅｉｎらによる米国特許第
５２９１７３７号明細書、Ｓｔｒａｕｂらによる米国特
許第５４５４２２７号明細書には、動力原単位の低減を
目的とした低純度酸素製造プロセスが記載されている。US Pat. No. 5,291,737 to Camberlein et al. And US Pat. No. 5,454,227 to Straub et al. Describe low purity oxygen production processes aimed at reducing power consumption.
【０００４】米国特許第５２９１７３７号明細書記載の
プロセスでは、製品酸素より酸素純度の高い液化酸素を
低圧蒸留塔から抜き出し、ポンプで圧縮した後、ｍｉｘ
ｉｎｇ ｃｏｌｕｍｎ（ミキシング塔）で原料空気の一
部と気液接触させることにより、原料空気と同程度の圧
力の低純度酸素を製造するようにしている。In the process described in US Pat. No. 5,291,737, liquefied oxygen having a higher oxygen purity than product oxygen is extracted from a low-pressure distillation column, compressed with a pump, and then mixed.
A low-purity oxygen having a pressure equivalent to that of the raw air is produced by bringing a part of the raw air into gas-liquid contact with an ing column (mixing tower).
【０００５】しかし、このプロセスでは、全空気量の約
３０％の空気をミキシング塔に導入して液化酸素と気液
接触させて液化させるため、高圧蒸留塔に供給する原料
空気量が減少する。その結果、高圧塔の上昇ガスが少な
くなり、主凝縮器で液化する量が減少するため、低圧蒸
留塔における還流窒素量が減少してＬ／Ｖが低下し、精
留効率が悪化して製品酸素の回収率が低下するととも
に、得られる窒素の純度も低下してしまう。However, in this process, about 30% of the total amount of air is introduced into the mixing tower and liquefied by gas-liquid contact with liquefied oxygen, so that the amount of raw air supplied to the high-pressure distillation tower is reduced. As a result, the amount of gas rising in the high-pressure column is reduced, and the amount of liquefaction in the main condenser is reduced. As a result, the amount of reflux nitrogen in the low-pressure distillation column is reduced, L / V is reduced, and the rectification efficiency is deteriorated. As the oxygen recovery rate decreases, the purity of the obtained nitrogen also decreases.
【０００６】すなわち、このプロセスでは、製品酸素の
圧縮動力は低減できるが、原料空気圧縮機の動力が増加
する。さらに、このプロセスでは、得られる窒素の純度
も低いため、ガス化複合発電（ＩＧＣＣ）のように、一
定純度以上の窒素を製品として必要とする設備には不適
当である。That is, in this process, the power for compressing product oxygen can be reduced, but the power for the raw air compressor increases. Further, this process has a low purity of the obtained nitrogen, and therefore is not suitable for equipment that requires nitrogen of a certain purity or higher as a product, such as integrated gasification combined cycle (IGCC).
【０００７】また、米国特許第５４５４２２７号明細書
記載のプロセスでは、低圧蒸留塔底部から抜き出した液
化酸素をポンプで圧縮してミキシング塔に供給し、原料
空気の一部と気液接触させるようにしている。この空気
には、膨張タービンで膨張させた空気と膨張バルブで減
圧させた空気とを使用している。In the process described in US Pat. No. 5,454,227, liquefied oxygen extracted from the bottom of the low-pressure distillation column is compressed by a pump, supplied to a mixing column, and brought into gas-liquid contact with a part of the raw air. ing. As the air, air expanded by an expansion turbine and air depressurized by an expansion valve are used.
【０００８】したがって、このプロセスにおいても、前
記同様に、高圧蒸留塔に供給する原料空気が減少するた
め、低圧蒸留塔に供給する還流窒素が減少し、製品回収
率が低下する。また、このプロセスでは、高圧に圧縮し
た原料空気の一部を膨張バルブで減圧してからミキシン
グ塔に供給するようにしているため、減圧による動力の
ロスを生じる。Accordingly, also in this process, as in the above, since the amount of feed air supplied to the high-pressure distillation column is reduced, the amount of reflux nitrogen supplied to the low-pressure distillation column is reduced, and the product recovery rate is reduced. Further, in this process, a part of the raw air compressed to a high pressure is reduced in pressure by the expansion valve and then supplied to the mixing tower, so that a power loss occurs due to the reduced pressure.
【０００９】そこで本発明は、比較的高圧力の低純度酸
素を製造するプロセスにおいて、酸素回収率の向上や圧
縮機に要する動力費の削減により原単位の低減が図れ、
さらに、同時に得られる窒素の純度低下も防止すること
ができる低純度酸素の製造方法及び装置を提供すること
を目的としている。Accordingly, the present invention can reduce the unit consumption by improving the oxygen recovery rate and reducing the power cost required for the compressor in the process of producing low-purity oxygen at a relatively high pressure.
It is another object of the present invention to provide a method and an apparatus for producing low-purity oxygen, which can prevent a decrease in the purity of nitrogen obtained at the same time.
【００１０】[0010]
【課題を解決するための手段】上記目的を達成するた
め、本発明の低純度酸素の製造方法は、高圧塔、低圧塔
及びミキシング塔を有する三塔式蒸留設備に原料空気を
導入して低温蒸留することにより、少なくとも低純度酸
素を製品として分離回収する低純度酸素の製造方法にお
いて、圧縮，精製，冷却した原料空気を前記高圧塔に導
入して第一窒素留分と第一酸素富化液留分とに分離する
第一蒸留工程と、該第一蒸留工程で分離した第一窒素留
分と第一酸素富化液留分とを前記低圧塔に導入して第二
窒素留分と第二酸素富化液留分とに分離する第二蒸留工
程と、前記第一酸素富化液留分を気化した後に前記ミキ
シング塔の下部に上昇ガスとして導入するとともに、前
記第二酸素富化液留分を昇圧した後に前記ミキシング塔
の上部に還流液として導入し、低純度酸素留分と塔底液
留分とに分離する第三蒸留工程と、該第三蒸留工程で分
離した低純度酸素留分を製品として回収する製品回収工
程とを含むことを特徴としている。In order to achieve the above object, the method for producing low-purity oxygen according to the present invention comprises introducing a raw air into a three-column distillation apparatus having a high-pressure column, a low-pressure column and a mixing column to reduce the temperature. In a method for producing low-purity oxygen, wherein at least low-purity oxygen is separated and recovered as a product by distillation, compressed, purified, and cooled raw material air is introduced into the high-pressure column to separate the first nitrogen fraction and the first oxygen-enriched air. A first distillation step of separating into a liquid fraction, and introducing the first nitrogen fraction and the first oxygen-enriched liquid fraction separated in the first distillation step into the low-pressure column to form a second nitrogen fraction. A second distillation step of separating into a second oxygen-enriched liquid fraction, and introducing the first oxygen-enriched liquid fraction into the lower portion of the mixing tower as a rising gas after vaporizing the second oxygen-enriched liquid fraction; After raising the pressure of the liquid fraction, a reflux liquid is formed at the top of the mixing tower. A third distillation step of introducing and separating into a low-purity oxygen fraction and a bottom liquid fraction, and a product recovery step of recovering the low-purity oxygen fraction separated in the third distillation step as a product. Features.
【００１１】さらに、本発明の低純度酸素の製造方法
は、前記第一酸素富化液留分の気化を前記第一窒素留分
との熱交換により行うことを特徴としている。また、気
化されてミキシング塔に導入される前記第一酸素富化液
留分を高圧塔の塔底から少なくとも１理論段上から抜き
出すこと、ミキシング塔に導入する前記第二酸素富化液
留分を低圧塔の塔底から少なくとも１理論段上から抜き
出すとともに、低圧塔の塔底部から高純度の酸素ガスを
抜き出すことを特徴としている。さらに、前記ミキシン
グ塔の塔底から抜き出した塔底液留分を該塔底液留分の
酸素濃度に対応する位置で前記低圧塔に導入すること、
前記ミキシング塔の中間部から液を抜き出し、該液の酸
素濃度に対応する位置で前記低圧塔に導入することを特
徴としている。Further, the method for producing low-purity oxygen of the present invention is characterized in that the first oxygen-enriched liquid fraction is vaporized by heat exchange with the first nitrogen fraction. Extracting the first oxygen-enriched liquid fraction vaporized and introduced into the mixing tower from at least one theoretical plate from the bottom of the high-pressure column; and introducing the second oxygen-enriched liquid fraction introduced into the mixing tower. Is extracted from at least one theoretical plate above the bottom of the low-pressure column, and high-purity oxygen gas is extracted from the bottom of the low-pressure column. Further, introducing the bottom liquid fraction extracted from the bottom of the mixing tower to the low-pressure column at a position corresponding to the oxygen concentration of the bottom liquid fraction,
A liquid is extracted from an intermediate portion of the mixing tower, and introduced into the low-pressure column at a position corresponding to the oxygen concentration of the liquid.
【００１２】また、本発明の低純度酸素の製造装置は、
圧縮，精製，冷却されて導入される原料空気を蒸留して
塔上部の第一窒素留分と塔下部の第一酸素富化液留分と
に分離する高圧塔と、該高圧塔で分離した第一窒素留分
と第一酸素富化液留分とを導入して蒸留することにより
塔上部の第二窒素留分と塔下部の第二酸素富化液留分と
に分離する低圧塔と、前記高圧塔から前記第一酸素富化
液留分を抜き出す第一酸素富化液留分抜出経路と、該第
一酸素富化液留分抜出経路に抜き出した第一酸素富化液
留分を気化するリボイラ／コンデンサと、前記低圧塔か
ら前記第二酸素富化液留分を抜き出す第二酸素富化液留
分抜出経路と、該第二酸素富化液留分抜出経路に抜き出
した第二酸素富化液留分を昇圧する液ポンプと、前記リ
ボイラ／コンデンサで気化した第一酸素富化留分及び前
記液ポンプで昇圧された第二酸素富化液留分とを導入し
て蒸留することにより塔上部の低純度酸素留分と塔底部
の塔底液留分とに分離するミキシング塔と、該ミキシン
グ塔で分離した前記低純度酸素留分を製品として回収す
る製品回収経路とを備えたことを特徴としている。Further, the apparatus for producing low-purity oxygen of the present invention comprises:
A high-pressure column in which the raw material air introduced after being compressed, purified and cooled is distilled to be separated into a first nitrogen fraction at the top of the column and a first oxygen-enriched liquid fraction at the bottom of the column, and the high-pressure column is used for separation. A low-pressure column that separates into a second nitrogen fraction at the top of the column and a second oxygen-enriched liquid fraction at the bottom of the column by introducing and distilling the first nitrogen fraction and the first oxygen-enriched liquid fraction; A first oxygen-enriched liquid fraction extraction path for extracting the first oxygen-enriched liquid fraction from the high-pressure column, and a first oxygen-enriched liquid extracted to the first oxygen-enriched liquid fraction extraction path Reboiler / condenser for vaporizing a fraction, a second oxygen-enriched liquid fraction withdrawal path for extracting the second oxygen-enriched liquid fraction from the low-pressure column, and a second oxygen-enriched liquid fraction withdrawal path A liquid pump for increasing the pressure of the second oxygen-enriched liquid fraction withdrawn with the first oxygen-enriched fraction vaporized by the reboiler / condenser and the liquid pump A mixing tower that separates into a low-purity oxygen fraction at the top of the tower and a bottoms liquid fraction at the bottom of the tower by introducing and distilling the obtained second oxygen-enriched liquid fraction, and separated by the mixing tower. A product recovery path for recovering the low-purity oxygen fraction as a product.
【００１３】さらに、本発明の低純度酸素の製造装置
は、前記第一酸素富化液留分抜出経路が高圧塔の塔底か
ら少なくとも１理論段上に設けられていること、前記第
二酸素富化液留分抜出経路が低圧塔の塔底から少なくと
も１理論段上に設けられるとともに、最下段精留段の下
に低圧塔底部に分離した高純度の酸素ガスを抜き出す高
純度酸素抜出経路が設けられていることを特徴としてい
る。Further, in the apparatus for producing low-purity oxygen of the present invention, the first oxygen-enriched liquid fraction extraction path is provided at least one theoretical plate above the bottom of the high-pressure column. An oxygen-enriched liquid fraction extraction path is provided at least one theoretical stage above the bottom of the low-pressure column, and high-purity oxygen that extracts high-purity oxygen gas separated at the bottom of the low-pressure column below the lowermost rectification stage It is characterized in that an extraction path is provided.
【００１４】また、前記ミキシング塔の塔底部に分離し
た塔底液留分を抜き出し、前記低圧塔の中部に還流液と
して導入する第一酸素還流経路を備えていること、前記
ミキシング塔の中段から液を抜き出し、前記低圧塔の中
部より下方の位置に還流液として導入する第二酸素還流
経路を備えていることを特徴とし、さらに、前記リボイ
ラ／コンデンサがドライタイプであることを特徴として
いる。Further, a first oxygen reflux path for extracting a bottom liquid fraction separated at the bottom of the mixing tower and introducing it as a reflux liquid into the center of the low-pressure tower is provided. It is characterized in that a second oxygen recirculation path for extracting the liquid and introducing it as a reflux liquid below the middle part of the low-pressure column is provided, and the reboiler / condenser is of a dry type.
【００１５】[0015]
【発明の実施の形態】図１は本発明の一形態例を示す系
統図である。この系統図に示す装置は、高圧塔１、低圧
塔２及びミキシング塔３を有するとともに、空気を低温
蒸留するための付帯設備である原料空気圧縮機４、前処
理設備５、主熱交換器６、主凝縮器７、過冷器８、リボ
イラ／コンデンサ９等の各種機器、各種弁及び配管を備
えた三塔式蒸留設備である。FIG. 1 is a system diagram showing one embodiment of the present invention. The apparatus shown in this system diagram has a high-pressure column 1, a low-pressure column 2, and a mixing column 3, and has a raw material air compressor 4, a pretreatment facility 5, and a main heat exchanger 6, which are auxiliary facilities for low-temperature distillation of air. , A main condenser 7, a subcooler 8, a reboiler / condenser 9, etc., and a three-tower distillation apparatus equipped with various valves and piping.
【００１６】以下、低純度酸素を製造する手順に基づい
て本形態例を説明する。まず、経路１０から吸入された
１０２０００Ｎｍ３／ｈの原料空気は、原料空気圧縮４
で６．０ｋｇ／ｃｍ２ abs．に圧縮され、アフタークー
ラー１１で４０℃に冷却された後、前処理設備５で二酸
化炭素や水分等の不純物を除去されて精製される。この
原料空気は、経路１２から経路１３と経路１４とに分岐
し、一方の経路１３に分岐した原料空気は、空気予冷器
１５を通ってからブロワー１６で更に圧縮され、アフタ
ークーラー１７及び空気予冷器１５で冷却される。さら
に、この原料空気は、経路１８から主熱交換器６を通っ
て中間温度に冷却された後、経路１９を通って前記ブロ
ワー１６に直結した膨張タービン２０に導入され、膨張
してプラントに必要な寒冷を発生する。膨張して低圧状
態となったこの原料空気は、経路２１を通って低圧塔２
の所定の位置に導入される。他方の経路１４に分岐した
原料空気は、主熱交換器６で露点温度付近まで冷却され
た後、経路２２を通って高圧塔１の下部に導入される。The present embodiment will be described below based on a procedure for producing low-purity oxygen. First, the raw material air of 102000 Nm 3 / h sucked from the passage 10 is compressed by the raw air compression 4
6.0 kg / cm 2 abs. After cooling to 40 ° C. in the aftercooler 11, the pretreatment equipment 5 removes impurities such as carbon dioxide and moisture to purify the product. The raw material air is branched from a path 12 to a path 13 and a path 14, and the raw material air branched to one path 13 is further compressed by a blower 16 after passing through an air precooler 15, and is further compressed by an aftercooler 17 and an air precooler. It is cooled in the vessel 15. Further, the feed air is cooled from the passage 18 through the main heat exchanger 6 to an intermediate temperature, and then introduced into the expansion turbine 20 directly connected to the blower 16 through the passage 19, expanded and required for the plant. It produces cold. The raw material air expanded to a low pressure state passes through a path 21 and passes through the low pressure tower 2.
Is introduced at a predetermined position. The raw material air branched to the other path 14 is cooled to near the dew point temperature in the main heat exchanger 6, and then introduced into the lower part of the high-pressure column 1 through the path 22.
【００１７】高圧塔１では、塔内を上昇するガスと、塔
頂部の主凝縮器７で凝縮して塔内を下降する液との気液
接触によって第一蒸留工程が行われ、塔頂部の第一窒素
留分と、塔底部の第一酸素富化液留分とに分離する。高
圧塔１の頂部から経路２３に抜き出された第一窒素留
分、即ち窒素ガスは、その一部が経路２４を通って主凝
縮器７に導入され、後述する低圧塔底部の第二酸素富化
液留分と熱交換することにより凝縮して液化窒素とな
り、経路２５に導出し、その一部が経路２６に分岐して
高圧塔１の頂部に還流液として戻される。また、経路２
３から経路２７に進んだ窒素ガスは、前記リボイラ／コ
ンデンサ９で高圧塔底部からの第一酸素富化液留分と熱
交換することにより凝縮して液化窒素となり、経路２８
に導出し、その一部が前記経路２６から高圧塔１の還流
液として戻される。In the high-pressure column 1, the first distillation step is performed by gas-liquid contact between the gas rising in the column and the liquid condensed in the main condenser 7 at the top and descending in the column. It is separated into a first nitrogen fraction and a first oxygen-enriched liquid fraction at the bottom of the column. A part of the first nitrogen fraction, that is, nitrogen gas, extracted from the top of the high-pressure column 1 to the path 23 through the path 24 is introduced into the main condenser 7, and the second oxygen fraction at the bottom of the low-pressure column, which will be described later. By heat exchange with the enriched liquid fraction, it is condensed to liquefied nitrogen, which is led out to a passage 25, and a part thereof is branched to a passage 26 and returned to the top of the high-pressure column 1 as a reflux liquid. Route 2
The nitrogen gas which has proceeded from 3 to the path 27 is condensed into liquefied nitrogen by exchanging heat with the first oxygen-enriched liquid fraction from the bottom of the high pressure column in the reboiler / condenser 9,
And a part thereof is returned from the passage 26 as a reflux liquid of the high-pressure column 1.
【００１８】還流液となる以外の液化窒素４７０００Ｎ
ｍ３／hは、前記経路２５，２８から経路２９に合流
し、前記過冷器８で冷却された後、経路３０を通り、膨
張弁３１で低圧塔２の圧力１．３ｋｇ／ｃｍ２ abs．に
減圧された後、経路３２を通って低圧塔２の頂部に還流
液として導入される。Liquefied nitrogen other than reflux liquid 47000N
m 3 / h joins the path 29 from the paths 25 and 28 and is cooled by the subcooler 8, passes through the path 30, passes through the path 30, and the pressure of the low-pressure tower 2 is 1.3 kg / cm 2 abs at the expansion valve 31 . After passing through the path 32, the liquid is introduced into the top of the low-pressure column 2 as a reflux liquid.
【００１９】一方、前記高圧塔１の底部に分離した酸素
分約４０％の第一酸素富化液留分は、経路３３に抜き出
されて経路３４と経路３５とに分岐する。経路３４に分
岐した２３０００Ｎｍ３／ｈの第一酸素富化液留分は、
過冷器８で冷却された後、経路３６を通り、膨張弁３７
で低圧塔２の圧力１．３ｋｇ／ｃｍ２ abs．に減圧さ
れ、経路３８を通って低圧塔２の中上部に還流液として
導入される。また、経路３３から経路３５に続く第一酸
素富化液留分抜出経路に分岐した２７４００Ｎｍ ３／ｈ
の第一酸素富化液留分は、膨張弁３９で２．６ｋｇ／ｃ
ｍ２ abs．に減圧された後、経路４０を経て前記リボイ
ラ／コンデンサ９に導入され、高圧塔頂部からの前記窒
素ガスと熱交換することによりガス化し、経路４１を通
って前記ミキシング塔３の底部に上昇ガスとして導入さ
れる。On the other hand, oxygen separated at the bottom of the high-pressure column 1
The first oxygen-enriched liquid fraction of about 40% is withdrawn to the passage 33.
Then, the path branches to a path 34 and a path 35. Minutes on path 34
23,000Nm3/ H of the primary oxygen-enriched liquid fraction
After being cooled by the subcooler 8, it passes through the path 36,
And the pressure of the low pressure tower 2 is 1.3 kg / cm2 abs. Decompressed
Through the passage 38 as a reflux liquid in the upper middle part of the low-pressure column 2.
be introduced. Also, the first acid following the route 33 to the route 35
27400Nm branched to the distillate extraction route 3/ H
Of the first oxygen-enriched liquid fraction at the expansion valve 39 is 2.6 kg / c
m2 abs. After the pressure has been reduced to
Into the condenser / condenser 9 from the top of the high pressure tower.
Gasification by heat exchange with raw gas
Is introduced into the bottom of the mixing tower 3 as rising gas.
It is.
【００２０】なお、本形態例では、リボイラ／コンデン
サ９として、液浸漬型ではなく、ドライ型のリボイラ／
コンデンサを使用している。すなわち、液浸漬型の場合
は、気化側の液体が液ヘッドによって過冷却状態となる
ため、この分、気化圧力を低くしなければならないが、
ドライタイプの場合には、このようなことがないので、
気化圧力を高めることができる。したがって、ミキシン
グ塔３に導入する第一酸素富化液留分の気化圧力を高く
することができるので、ミキシング塔３の運転圧力を高
めることができ、最終的にミキシング塔３から回収する
製品低純度酸素ガスの圧力を高くすることができる。し
かも、ドライタイプは、液浸漬型に比べて保有液量が少
ないので、装置の起動時間を短縮できる効果もある。In this embodiment, the reboiler / condenser 9 is not a liquid immersion type but a dry type reboiler / condenser.
A capacitor is used. That is, in the case of the liquid immersion type, since the liquid on the vaporization side is supercooled by the liquid head, the vaporization pressure must be reduced accordingly,
In the case of dry type, there is no such thing,
The vaporization pressure can be increased. Therefore, the vaporization pressure of the first oxygen-enriched liquid fraction introduced into the mixing tower 3 can be increased, so that the operating pressure of the mixing tower 3 can be increased, and the product recovered from the mixing tower 3 can be reduced. The pressure of the pure oxygen gas can be increased. In addition, the dry type has a smaller amount of retained liquid than the liquid immersion type, and thus has the effect of shortening the startup time of the apparatus.
【００２１】前記低圧塔２では、前記経路３２，３８か
らそれぞれ導入される還流液と、塔底部の主凝縮器７で
気化した上昇ガスとの気液接触によって第二蒸留工程が
行われ、塔頂部の第二窒素留分と、塔底部の第二酸素富
化液留分とに分離する。In the low-pressure column 2, a second distillation step is performed by gas-liquid contact between the reflux liquid introduced from each of the channels 32 and 38 and the rising gas vaporized in the main condenser 7 at the bottom of the column. It is separated into a second nitrogen fraction at the top and a second oxygen-enriched liquid fraction at the bottom of the column.
【００２２】塔頂部からは、第二窒素留分である窒素ガ
ス７９６５０Ｎｍ３／ｈが経路４２に抜き出され、過冷
器８での熱交換により昇温した後、経路４３を通って主
熱交換器６で原料空気と熱交換することにより常温まで
昇温し、経路４４から製品窒素として抜き出される。本
形態例のプロセスでは、原料空気の全量を高圧塔１に導
入していることから、低圧塔２の頂部還流液化窒素量を
多くすることができるため、低圧塔頂部の窒素濃度は９
９．３％であり、製品窒素ガスとして十分に使用可能で
ある。From the top of the tower, nitrogen gas 79650 Nm 3 / h, which is a second nitrogen fraction, is withdrawn through a passage 42, heated by heat exchange in a subcooler 8, and then passed through a passage 43 to obtain main heat. The heat is exchanged with the raw material air in the exchanger 6 to raise the temperature to room temperature, and is extracted from the path 44 as product nitrogen. In the process of the present embodiment, since the entire amount of the raw material air is introduced into the high-pressure column 1, the amount of liquefied nitrogen refluxed at the top of the low-pressure column 2 can be increased.
It is 9.3% and can be sufficiently used as product nitrogen gas.
【００２３】低圧塔２の底部の第二酸素富化液留分は、
酸素濃度９８％の液化酸素であり、６６０００Ｎｍ３／
ｈが第二酸素富化液留分抜出経路である経路４５に抜き
出され、液ポンプ４６で２．６ｋｇ／ｃｍ２ abs．に圧
縮された後、経路４７を通ってミキシング塔３の頂部に
還流液として供給される。The second oxygen-enriched liquid fraction at the bottom of the low pressure column 2 is
Oxygen concentration was 98% of the liquid oxygen, 66000Nm 3 /
h is withdrawn through a passage 45 which is a second oxygen-enriched liquid fraction withdrawal passage, and 2.6 kg / cm 2 abs. After being compressed, the mixture is supplied to the top of the mixing tower 3 through a path 47 as a reflux liquid.
【００２４】ミキシング塔３では、前記経路４１から導
入された上昇ガスと、上記経路４７から導入された還流
液とが気液接触することにより第三蒸留工程が行われ、
塔頂部の低純度酸素留分と、塔底部の塔底液留分とに分
離する。塔頂部の低純度酸素留分は、酸素濃度９５％の
低純度酸素であり、製品回収経路となる頂部の経路４８
から２２３５０Ｎｍ３／ｈが抜き出され、主熱交換器６
で常温まで昇温した後、経路４９を通ってブロワー５０
で所定圧力に圧縮されて経路５１から取り出される。In the mixing tower 3, a third distillation step is performed by bringing the ascending gas introduced from the path 41 into a gas-liquid contact with the reflux liquid introduced from the path 47,
It is separated into a low-purity oxygen fraction at the top and a bottoms liquid fraction at the bottom. The low-purity oxygen fraction at the top of the tower is low-purity oxygen having an oxygen concentration of 95%, and is a top path 48 which is a product recovery path.
22350 Nm 3 / h from the main heat exchanger 6
After raising the temperature to normal temperature through
Is compressed to a predetermined pressure and taken out of the path 51.
【００２５】ミキシング塔３の底部から第一酸素還流経
路である経路５２に抜き出された塔底液留分は、膨張弁
５３で低圧塔２の圧力に減圧された後、経路５４を通
り、塔底液留分の酸素濃度に対応した位置の低圧塔中部
に導入される。また、ミキシング塔３の中間部からは、
塔内を下降する液の一部が第二酸素還流経路である経路
５５に抜き出され、膨張弁５６で低圧塔２の圧力に減圧
された後、経路５７を通り、該液の酸素濃度に対応した
位置の低圧塔中部より下方に導入される。The bottom liquid fraction withdrawn from the bottom of the mixing tower 3 to the path 52, which is the first oxygen reflux path, is reduced to the pressure of the low-pressure tower 2 by the expansion valve 53, and then passes through the path 54. It is introduced into the lower pressure column at a position corresponding to the oxygen concentration of the bottom liquid fraction. Also, from the middle part of the mixing tower 3,
A part of the liquid descending in the column is withdrawn to a path 55 which is a second oxygen recirculation path, reduced to the pressure of the low-pressure tower 2 by an expansion valve 56, and then passed through a path 57 to the oxygen concentration of the liquid. It is introduced below the middle part of the low pressure column at the corresponding position.
【００２６】上述のように、高圧塔１から抜き出した第
一酸素富化液留分を気化してミキシング塔３の上昇ガス
として用いることにより、原料空気のほとんどを高圧塔
１に供給することができるので、低圧塔２の頂部還流液
化窒素量を多くすることができる。これにより、低圧塔
２のＬ／Ｖが改善されて精留効率が向上し、製品低純度
酸素の回収率が増加するとともに、低圧塔２から抜き出
す窒素の純度も向上させることができる。したがって、
本形態例プロセスは、大量の低純度酸素と共に、一定純
度以上の窒素ガスを大量に必要とするガス化複合発電に
も好適に用いることができる。As described above, most of the raw material air can be supplied to the high-pressure column 1 by vaporizing the first oxygen-enriched liquid fraction extracted from the high-pressure column 1 and using it as the rising gas of the mixing column 3. Therefore, the amount of liquefied nitrogen at the top of the low-pressure column 2 can be increased. Thereby, the L / V of the low-pressure column 2 is improved, the rectification efficiency is improved, the recovery rate of the product low-purity oxygen is increased, and the purity of the nitrogen extracted from the low-pressure column 2 can be improved. Therefore,
The process of this embodiment can be suitably used for combined gasification power generation, which requires a large amount of nitrogen gas of a certain purity or more together with a large amount of low-purity oxygen.
【００２７】また、高圧塔１からミキシング塔３に供給
する第一酸素富化液留分の気化を、高圧塔１から抜き出
した第一窒素留分との熱交換で行うことにより、第一酸
素富化液留分の気化を、他の加熱源を用意することなく
効率よく行えるとともに、第一窒素留分を液化させて高
圧塔１や低圧塔２の還流液として使用することができ
る。さらに、ミキシング塔３から抜き出した液を、低圧
塔２の酸素濃度に対応した位置に供給することにより、
低圧塔２の運転を乱すことなく安定した効率のよい蒸留
操作を行うことができる。The first oxygen-enriched liquid fraction to be supplied from the high-pressure column 1 to the mixing column 3 is vaporized by heat exchange with the first nitrogen fraction extracted from the high-pressure column 1 so that the first oxygen-enriched liquid fraction is vaporized. Evaporation of the enriched liquid fraction can be performed efficiently without preparing another heating source, and the first nitrogen fraction can be liquefied and used as a reflux liquid of the high-pressure column 1 or the low-pressure column 2. Further, by supplying the liquid extracted from the mixing tower 3 to a position corresponding to the oxygen concentration of the low-pressure tower 2,
A stable and efficient distillation operation can be performed without disturbing the operation of the low pressure column 2.
【００２８】ここで、本形態例に示すプロセスと、従来
例として前記米国特許第５２９１７３７号明細書記載の
プロセスとにおいて、同条件の低純度酸素を製造する場
合のシミュレーションを行った結果を表１に示す。な
お、酸素製造原単位には、従来例と条件を合わせるた
め、酸素を６８ｋｇ／ｃｍ２ abs．まで昇圧するための
ブロワー５０の動力も含めている。Here, Table 1 shows the results of simulations for producing low-purity oxygen under the same conditions in the process shown in the present embodiment and the process described in US Pat. No. 5,291,737 as a conventional example. Shown in In addition, in order to match the condition with the conventional example, oxygen is 68 kg / cm 2 abs. The power of the blower 50 for raising the pressure to the maximum is also included.
【００２９】[0029]
【表１】 [Table 1]
【００３０】上記シミュレーションでは、全ての蒸留塔
に棚段を使用した場合で計算を行ったが、高圧塔１，低
圧塔２，ミキシング塔３の少なくとも１つに充填物を使
用することにより、蒸留塔の圧力損失を少なくすること
ができるので、さらに酸素製造原単位を低減させること
ができる。In the above simulation, the calculation was performed in the case where trays were used for all the distillation columns, but the distillation was performed by using a packing material in at least one of the high-pressure column 1, the low-pressure column 2, and the mixing column 3. Since the pressure loss in the column can be reduced, the unit oxygen production unit can be further reduced.
【００３１】また、本形態例では、高圧塔１の第一酸素
富化液留分の一部をミキシング塔３に供給するようにし
ているが、リボイラ／コンデンサ９における炭化水素の
濃縮を防止するため、図１に破線で示すように、高圧塔
１の塔底から少なくとも１理論段上の精留段１ａから経
路３５ａを通して液を抜き出すようにしてもよい。In this embodiment, a part of the first oxygen-enriched liquid fraction in the high-pressure column 1 is supplied to the mixing column 3, but the concentration of hydrocarbons in the reboiler / condenser 9 is prevented. Therefore, as shown by the broken line in FIG. 1, the liquid may be extracted from the bottom of the high-pressure column 1 through the path 35a from the rectification stage 1a at least one theoretical stage.
【００３２】また、図２に示すように、ミキシング塔３
に還流液として導入する液も、低圧塔２の塔底から数段
上の精留段２ａに設けた経路４５ａで抜き出すととも
に、最下段の精留段２ｂより下に設けた経路（高純度酸
素抜出経路）５８から主熱交換器６，経路５９を通し
て、純度の高い酸素ガスを抜き出すこともできる。As shown in FIG. 2, the mixing tower 3
The liquid to be introduced as a reflux liquid into the rectification stage 2a is withdrawn from the bottom of the low-pressure column 2 through a passage 45a provided in the rectification stage 2a several stages above, and a liquid (high-purity oxygen) provided below the bottom rectification stage 2b. High-purity oxygen gas can also be extracted from the extraction path 58 through the main heat exchanger 6 and the path 59.
【００３３】これにより、ミキシング塔３から抜き出す
低純度の酸素と、低圧塔２から抜き出す高純度の酸素と
の純度の異なる２種類の製品酸素を得ることができるの
で、大量の低純度酸素と少量の高純度酸素とを必要とす
る設備、例えば、コレックス（ＣＯＲＥＸ）製鋼法を基
にした新しいグラスルーツ製鋼所等の用途に好適であ
る。As a result, two types of product oxygen having different purities, that is, low-purity oxygen extracted from the mixing tower 3 and high-purity oxygen extracted from the low-pressure tower 2 can be obtained. It is suitable for use in equipment requiring high-purity oxygen, such as a new grassroots steel mill based on the COREX steelmaking method.
【００３４】[0034]
【発明の効果】以上説明したように、本発明によれば、
比較的圧力が高い低純度酸素を効率よく製造でき、回収
率の向上や圧縮機に要する動力費の削減により原単位の
低減が図れる。さらに、比較的高純度の窒素も同時に製
造することが可能であり、低純度の酸素と高純度の酸素
とを同時に製造することも可能である。As described above, according to the present invention,
Low-purity oxygen with a relatively high pressure can be efficiently produced, and the unit consumption can be reduced by improving the recovery rate and reducing the power cost required for the compressor. Further, relatively high purity nitrogen can be produced at the same time, and low-purity oxygen and high-purity oxygen can be produced simultaneously.
【図１】 本発明の一形態例を示す系統図である。FIG. 1 is a system diagram showing one embodiment of the present invention.
【図２】 変形例を示す要部の系統図である。FIG. 2 is a system diagram of a main part showing a modification.
１…高圧塔、２…低圧塔、３…ミキシング塔、４…原料
空気圧縮機、５…前処理設備、６…主熱交換器、７…主
凝縮器、８…過冷器、９…リボイラ／コンデンサ、１５
…空気予冷器、１６…ブロワー、２０…膨張タービン、
３１，３７，３９…膨張弁、５０…ブロワー、５３，５
６…膨張弁DESCRIPTION OF SYMBOLS 1 ... High pressure tower, 2 ... Low pressure tower, 3 ... Mixing tower, 4 ... Raw material air compressor, 5 ... Pretreatment equipment, 6 ... Main heat exchanger, 7 ... Main condenser, 8 ... Supercooler, 9 ... Reboiler / Capacitor, 15
... air precooler, 16 ... blower, 20 ... expansion turbine,
31, 37, 39: expansion valve, 50: blower, 53, 5
6 ... Expansion valve
Claims (12)
る三塔式蒸留設備に原料空気を導入して低温蒸留するこ
とにより、少なくとも低純度酸素を製品として分離回収
する低純度酸素の製造方法において、圧縮，精製，冷却
した原料空気を前記高圧塔に導入して第一窒素留分と第
一酸素富化液留分とに分離する第一蒸留工程と、該第一
蒸留工程で分離した第一窒素留分と第一酸素富化液留分
とを前記低圧塔に導入して第二窒素留分と第二酸素富化
液留分とに分離する第二蒸留工程と、前記第一酸素富化
液留分を気化した後に前記ミキシング塔の下部に上昇ガ
スとして導入するとともに、前記第二酸素富化液留分を
昇圧した後に前記ミキシング塔の上部に還流液として導
入し、低純度酸素留分と塔底液留分とに分離する第三蒸
留工程と、該第三蒸留工程で分離した低純度酸素留分を
製品として回収する製品回収工程とを含むことを特徴と
する低純度酸素の製造方法。1. A low-purity oxygen production method for separating and recovering at least low-purity oxygen as a product by introducing raw air into a three-column distillation apparatus having a high-pressure tower, a low-pressure tower, and a mixing tower and performing low-temperature distillation. A first distillation step of introducing compressed, purified and cooled raw material air into the high-pressure column to separate it into a first nitrogen fraction and a first oxygen-enriched liquid fraction, and a second distillation step separated in the first distillation step. A second distillation step of introducing a mononitrogen fraction and a first oxygen-enriched liquid fraction into the low-pressure column to separate it into a second nitrogen fraction and a second oxygen-enriched liquid fraction; After evaporating the enriched liquid fraction, it is introduced as a rising gas into the lower part of the mixing tower, and after increasing the pressure of the second oxygen-enriched liquid fraction, it is introduced as a reflux liquid into the upper part of the mixing tower to obtain a low-purity oxygen. A third distillation step of separating into a fraction and a bottoms fraction, A product recovery step of recovering a low-purity oxygen fraction separated in the distillation step as a product.
第一窒素留分との熱交換により行うことを特徴とする請
求項１記載の低純度酸素の製造方法。2. The method for producing low-purity oxygen according to claim 1, wherein the first oxygen-enriched liquid fraction is vaporized by heat exchange with the first nitrogen fraction.
る第一酸素富化液留分が、前記高圧塔の塔底から少なく
とも１理論段上から抜き出されることを特徴とする請求
項１記載の低純度酸素の製造方法。3. The high-pressure column according to claim 1, wherein the first oxygen-enriched liquid fraction vaporized and introduced into the mixing column is withdrawn from at least one theoretical plate at the bottom of the high-pressure column. Method for producing low-purity oxygen.
化液留分を、前記低圧塔の塔底から少なくとも１理論段
上から抜き出すとともに、前記低圧塔の塔底部から高純
度の酸素ガスを抜き出すことを特徴とする請求項１記載
の低純度酸素の製造方法。4. A second oxygen-enriched liquid fraction introduced into the mixing tower is withdrawn from the bottom of the low-pressure column from at least one theoretical plate, and high-purity oxygen gas is removed from the bottom of the low-pressure column. The method for producing low-purity oxygen according to claim 1, wherein the oxygen is extracted.
塔底液留分を、該塔底液留分の酸素濃度に対応する位置
で前記低圧塔に導入することを特徴とする請求項１記載
の低純度酸素の製造方法。5. The low pressure column according to claim 1, wherein the bottom liquid fraction extracted from the bottom of the mixing tower is introduced into the low pressure column at a position corresponding to the oxygen concentration of the bottom liquid fraction. Method for producing low-purity oxygen.
出し、該液の酸素濃度に対応する位置で前記低圧塔に導
入することを特徴とする請求項１記載の低純度酸素の製
造方法。6. The method for producing low-purity oxygen according to claim 1, wherein a liquid is withdrawn from an intermediate portion of said mixing tower and introduced into said low-pressure column at a position corresponding to the oxygen concentration of said liquid.
空気を蒸留して塔上部の第一窒素留分と塔下部の第一酸
素富化液留分とに分離する高圧塔と、該高圧塔で分離し
た第一窒素留分と第一酸素富化液留分とを導入して蒸留
することにより塔上部の第二窒素留分と塔下部の第二酸
素富化液留分とに分離する低圧塔と、前記高圧塔から前
記第一酸素富化液留分を抜き出す第一酸素富化液留分抜
出経路と、該第一酸素富化液留分抜出経路に抜き出した
第一酸素富化液留分を気化するリボイラ／コンデンサ
と、前記低圧塔から前記第二酸素富化液留分を抜き出す
第二酸素富化液留分抜出経路と、該第二酸素富化液留分
抜出経路に抜き出した第二酸素富化液留分を昇圧する液
ポンプと、前記リボイラ／コンデンサで気化した第一酸
素富化留分及び前記液ポンプで昇圧された第二酸素富化
液留分とを導入して蒸留することにより塔上部の低純度
酸素留分と塔底部の塔底液留分とに分離するミキシング
塔と、該ミキシング塔で分離した前記低純度酸素留分を
製品として回収する製品回収経路とを備えたことを特徴
とする低純度酸素の製造装置。7. A high-pressure column for distilling compressed, purified, cooled and introduced raw air into a first nitrogen fraction at the top of the column and a first oxygen-enriched liquid fraction at the bottom of the column, By introducing and distilling the primary nitrogen fraction and the primary oxygen-enriched liquid fraction separated in the high-pressure column, a second nitrogen fraction at the top of the column and a second oxygen-enriched liquid fraction at the bottom of the column are formed. A low-pressure column to be separated, a first oxygen-enriched liquid fraction extraction path for extracting the first oxygen-enriched liquid fraction from the high-pressure column, and a first oxygen-enriched liquid fraction extraction path extracted from the first oxygen-enriched liquid fraction extraction path. A reboiler / condenser for evaporating the one oxygen-enriched liquid fraction, a second oxygen-enriched liquid fraction withdrawal path for extracting the second oxygen-enriched liquid fraction from the low-pressure column, and the second oxygen-enriched liquid A liquid pump for increasing the pressure of the second oxygen-enriched liquid fraction withdrawn to the fraction withdrawal path, and a first oxygen-enriched fraction vaporized by the reboiler / condenser and the liquid A mixing tower that separates a low-purity oxygen fraction at the top of the tower and a bottoms liquid fraction at the bottom of the tower by introducing and distilling the second oxygen-enriched liquid fraction pressurized by a pump; and And a product recovery path for recovering the low-purity oxygen fraction separated in step (1) as a product.
記高圧塔の塔底から少なくとも１理論段上に設けられて
いることを特徴とする請求項７記載の低純度酸素の製造
装置。8. The low-purity oxygen purifying apparatus according to claim 7, wherein the first oxygen-enriched liquid fraction extraction path is provided at least one theoretical plate above the bottom of the high-pressure column. manufacturing device.
記低圧塔の塔底から少なくとも１理論段上に設けられて
いるとともに、最下段精留段の下に低圧塔底部に分離し
た高純度の酸素ガスを抜き出す高純度酸素抜出経路が設
けられていることを特徴とする請求項７記載の低純度酸
素の製造装置。9. The second oxygen-enriched liquid fraction withdrawal path is provided at least one theoretical plate above the bottom of the low-pressure column, and is provided at the bottom of the low-pressure column below the lowermost rectification stage. 8. The apparatus for producing low-purity oxygen according to claim 7, further comprising a high-purity oxygen extracting path for extracting the separated high-purity oxygen gas.
塔底液留分を抜き出し、前記低圧塔の中部に還流液とし
て導入する第一酸素還流経路を備えたことを特徴とする
請求項７記載の低純度酸素の製造装置。10. The apparatus according to claim 7, further comprising a first oxygen reflux path for extracting a bottom liquid fraction separated at the bottom of the mixing tower and introducing it as a reflux liquid into the center of the low-pressure column. Low purity oxygen production equipment.
出し、前記低圧塔の中部より下方の位置に還流液として
導入する第二酸素還流経路を備えたことを特徴とする請
求項７記載の低純度酸素の製造装置。11. The low-purity low-purity system according to claim 7, further comprising a second oxygen reflux path for extracting a liquid from the middle stage of the mixing tower and introducing the liquid as a reflux liquid at a position below the center of the low-pressure column. Oxygen production equipment.
イプであることを特徴とする請求項７記載の低純度酸素
の製造装置。12. The apparatus for producing low-purity oxygen according to claim 7, wherein said reboiler / condenser is of a dry type.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP06157499A JP4177507B2 (en) | 1999-03-09 | 1999-03-09 | Method and apparatus for producing low purity oxygen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP06157499A JP4177507B2 (en) | 1999-03-09 | 1999-03-09 | Method and apparatus for producing low purity oxygen |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2000258054A true JP2000258054A (en) | 2000-09-22 |
| JP4177507B2 JP4177507B2 (en) | 2008-11-05 |
Family
ID=13175043
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP06157499A Expired - Lifetime JP4177507B2 (en) | 1999-03-09 | 1999-03-09 | Method and apparatus for producing low purity oxygen |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP4177507B2 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007516405A (en) * | 2003-11-10 | 2007-06-21 | レール・リキード−ソシエテ・アノニム・ア・ディレクトワール・エ・コンセイユ・ドゥ・スールベイランス・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 facility for supplying high purity oxygen by cryogenic distillation of air |
| JP2010286216A (en) * | 2009-06-15 | 2010-12-24 | Taiyo Nippon Sanso Corp | Air separation method and device |
| CN104964516A (en) * | 2015-07-10 | 2015-10-07 | 杭州杭氧股份有限公司 | Partly-integrated type air separation device matched with IGCC power plant and method achieved through partly-integrated type air separation device |
| EP3557166A1 (en) | 2018-04-19 | 2019-10-23 | Linde Aktiengesellschaft | Method for the low-temperature decomposition of air and air separation plant |
| RU2778193C2 (en) * | 2018-04-19 | 2022-08-15 | Линде Акциенгезельшафт | Method for cryogenic air separation and air separation installation |
-
1999
- 1999-03-09 JP JP06157499A patent/JP4177507B2/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007516405A (en) * | 2003-11-10 | 2007-06-21 | レール・リキード−ソシエテ・アノニム・ア・ディレクトワール・エ・コンセイユ・ドゥ・スールベイランス・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 facility for supplying high purity oxygen by cryogenic distillation of air |
| JP2010286216A (en) * | 2009-06-15 | 2010-12-24 | Taiyo Nippon Sanso Corp | Air separation method and device |
| CN104964516A (en) * | 2015-07-10 | 2015-10-07 | 杭州杭氧股份有限公司 | Partly-integrated type air separation device matched with IGCC power plant and method achieved through partly-integrated type air separation device |
| EP3557166A1 (en) | 2018-04-19 | 2019-10-23 | Linde Aktiengesellschaft | Method for the low-temperature decomposition of air and air separation plant |
| RU2778193C2 (en) * | 2018-04-19 | 2022-08-15 | Линде Акциенгезельшафт | Method for cryogenic air separation and air separation installation |
| US11602713B2 (en) | 2018-04-19 | 2023-03-14 | Linde Aktiengesellschaft | Method for cryogenic separation of air, and air separation plant |
Also Published As
| Publication number | Publication date |
|---|---|
| JP4177507B2 (en) | 2008-11-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP5425100B2 (en) | Cryogenic air separation method and apparatus | |
| JP4331460B2 (en) | Method and apparatus for producing krypton and / or xenon by low temperature air separation | |
| JPH06207775A (en) | Low-temperature air separating method for manufacturing nitrogen having no carbon monoxide | |
| JP2001263935A (en) | Method for separating air and air separator using the same | |
| JPH102664A (en) | Low temperature distillating method for air flow of compressed raw material for manufacturing oxygen products of low purity and high purity | |
| NO169977B (en) | PROCEDURE FOR SEPARATING AIR BY CRYOGEN DISTILLATION | |
| JP5307055B2 (en) | Nitrogen and oxygen production method and nitrogen and oxygen production apparatus. | |
| JPH06257939A (en) | Distilling method at low temperature of air | |
| JPS6367636B2 (en) | ||
| JP5032407B2 (en) | Nitrogen production method and apparatus | |
| JPH07151458A (en) | Method and equipment for preparing gaseous oxygen and/or nitrogen under pressure | |
| JP7355980B1 (en) | Ultra-high purity oxygen production method and ultra-high purity oxygen production equipment | |
| JPH10132458A (en) | Method and equipment for producing oxygen gas | |
| JPH1163810A (en) | Method and device for manufacturing low purity oxygen | |
| JP4177507B2 (en) | Method and apparatus for producing low purity oxygen | |
| JP4230213B2 (en) | Air liquefaction separation apparatus and method | |
| JPH07151459A (en) | Method and equipment for preparing at least one gas from airunder pressure | |
| JP4401999B2 (en) | Air separation method and air separation device | |
| JP3748677B2 (en) | Method and apparatus for producing low purity oxygen | |
| JP3414947B2 (en) | Argon purification method and air separation device | |
| JP5027173B2 (en) | Argon production method and apparatus thereof | |
| JP4577977B2 (en) | Air liquefaction separation method and apparatus | |
| JPH11173753A (en) | Method and device for manufacturing nitrogen and argon from air | |
| JP2859663B2 (en) | Nitrogen gas and oxygen gas production equipment | |
| JPH11325716A (en) | Separation of air |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20060301 |
|
| A977 | Report on retrieval |
Free format text: JAPANESE INTERMEDIATE CODE: A971007 Effective date: 20080213 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20080226 |
|
| A521 | Written amendment |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20080417 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20080729 |
|
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20080822 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20110829 Year of fee payment: 3 |
|
| R150 | Certificate of patent or registration of utility model |
Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20110829 Year of fee payment: 3 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20110829 Year of fee payment: 3 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20120829 Year of fee payment: 4 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20120829 Year of fee payment: 4 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20120829 Year of fee payment: 4 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130829 Year of fee payment: 5 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130829 Year of fee payment: 5 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| EXPY | Cancellation because of completion of term |