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JP4150102B2 - Air liquefaction separation method and apparatus - Google Patents
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JP4150102B2 - Air liquefaction separation method and apparatus - Google Patents

Air liquefaction separation method and apparatus Download PDF

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Publication number
JP4150102B2
JP4150102B2 JP13887598A JP13887598A JP4150102B2 JP 4150102 B2 JP4150102 B2 JP 4150102B2 JP 13887598 A JP13887598 A JP 13887598A JP 13887598 A JP13887598 A JP 13887598A JP 4150102 B2 JP4150102 B2 JP 4150102B2
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air
oxygen
low
raw material
purity oxygen
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JPH11325718A (en
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輝二 金子
陽子 深津
忠雄 比留間
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Nippon Sanso Holdings Corp
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    • 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
    • F25J3/04636—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 hybrid air separation unit, e.g. combined process by cryogenic separation and non-cryogenic separation techniques
    • 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
    • F25J3/04018—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 main 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04969—Retrofitting or revamping of an existing air fractionation unit
    • 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
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with the feed stream
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/24—Multiple compressors or compressor stages in parallel
    • 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
    • F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/50—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen

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  • 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

【０００１】
【発明の属する技術分野】
本発明は、空気液化分離方法及び装置に関し、詳しくは、製品酸素の需要変動に応じて酸素の生産量を増減することができる空気液化分離方法及び装置に関する。
【０００２】
【従来の技術及び発明が解決しようとする課題】
通常の空気液化分離装置において、装置の運転時間の１／２以下、あるいは１／３以下の頻度で酸素需要量が増加する場合、装置の能力をピーク値に合わせて製作すると、平均的な製造量のときの運転状態は、装置にとっては減量運転になる。さらに、酸素需要量が平均値以下になった場合には、より大きな減量領域での運転となるため、生産効率が悪化し、結果として電力消費の点で効率の悪い運転となる。一般的に、空気液化分離装置における空気圧縮機の減量限界や精留塔の減量限界から考えると、定格生産量に対する最小減量運転の生産量は、７５％程度までとなる。
【０００３】
一方、酸素ガスを大量に使用する製鉄工業や化学工業では、大型の空気液化分離装置を設置して酸素ガスを供給しているが、酸素ガスの需要は、操業計画，操業状態，曜日，時間帯等により大きく変動する。このため、需要減少時には、製品酸素ガスの一部（余剰分）を液化窒素等と熱交換させることにより液化して貯留し、需要増大時には貯留した液化酸素を気化して供給するようにした装置を設置することがある。しかしながら、このような特殊な装置は、あらかじめこれに対応した設計しておくか、既存の設備に大掛かりな改造を施す必要があり、設備コストの点で大きな問題が発生する。
【０００４】
そこで本発明は、通常の空気液化分離装置に簡単な設備を付加するだけで酸素の生産量を増大することができる空気液化分離方法及び装置を提供することを目的としている。
【０００５】
【課題を解決するための手段】
上記目的を達成するため、本発明の空気液化分離方法は、原料空気を圧縮・冷却・液化・精留してその成分ガスを得る空気液化分離方法において，原料空気を圧縮する原料空気圧縮機が吸入する大気空気に、付設した低純度の酸素を発生する装置で発生した低純度の酸素を添加混合して酸素分の多い原料空気とし，これを圧縮，冷却して液化精留を行うことにより、少なくとも酸素を製品として得ることを特徴としている。
【０００６】
さらに、本発明の空気液化分離方法は、前記酸素分の多い原料空気の酸素濃度を、大気の酸素濃度以上で、３０体積％以下とすること、前記低純度の酸素が、圧力変動吸着分離式酸素発生装置により製造され、その酸素濃度が８０〜９５体積％の低純度酸素であること、前記製品として得る酸素の需要量の変動に応じて，前記圧力変動吸着分離式酸素発生装置の運転を増量運転，減量運転又は運転停止することにより、前記大気空気に添加混合する低純度酸素の供給量を調節することを特徴としている。
【０００７】
また、本発明の空気液化分離装置は、大気空気からなる原料空気を圧縮する原料空気圧縮機と、該圧縮機で圧縮された圧縮空気を精製する吸着器と、該吸着器で精製された圧縮精製空気を冷却する熱交換器と、該熱交換器で冷却された圧縮精製冷却空気を液化・精留する精留塔を備え、前記原料空気の成分ガスを液化精留分離し、少なくとも酸素を製品として採取する空気液化精留分離装置において、低純度の酸素を発生する装置を付設するとともに、該装置で発生した低純度の酸素を導出する導出管を、前記原料空気圧縮機の大気空気吸入側（吸入系統）に連結したことを特徴としている。
【０００８】
さらに、本発明の空気液化分離装置は、前記低純度の酸素を発生する装置が，圧力変動吸着分離式酸素発生装置であり、該圧力変動吸着分離式酸素発生装置から導出される低純度の酸素を昇圧するための酸素ブロワーを備えていること、あるいは、低純度の酸素を昇圧する手段を介さずに、低純度の酸素を導出する導出管を前記原料空気圧縮機の大気空気吸入側（吸入系統）に連結したこと、また、前記圧力変動吸着分離式酸素発生装置から低純度の酸素を導出する導出管を、前記原料空気圧縮機が吸入する大気空気の吸入フィルターボックス又は原料空気吸入管に連結したことを特徴としている。
【０００９】
【発明の実施の形態】
図１は、本発明の空気液化分離装置の一形態例を示す概略系統図である。この空気液化分離装置は、製品として酸素と窒素とを採取するものであって、通常の空気液化分離装置と同様の構成の空気液化分離部１０と、該空気液化分離部１０に低純度酸素を供給する低純度酸素発生部２０とを有している。
【００１０】
空気液化分離部１０における通常の運転では、空気フィルター１１から吸入した大気空気（原料空気）を原料空気圧縮機１２で所定圧力に圧縮し、圧縮した圧縮空気を図示しない吸着器に導入して精製した後、この圧縮精製空気をコールドボックス１３内に導入して冷却・液化・精留することにより、経路１４から製品酸素が、経路１５から製品窒素がそれぞれ採取され、製品圧縮機１４ａ，１５ａにより圧送される。
【００１１】
なお、コールドボックス１３内には、熱交換器や精留塔，凝縮器，膨張タービン等の周知の機器が設けられており、周知の深冷分離法によって大気の成分ガスである窒素や酸素が分離される。
【００１２】
前記低純度酸素発生部２０は、大気空気よりも高濃度で酸素を含有する低純度の酸素を発生させることができれば、各種のものを用いることができ、例えば、酸素ＰＳＡ装置と呼ばれる圧力変動吸着分離式酸素発生装置や膜式酸素濃縮装置のように、大気空気を原料として低純度酸素を発生させる装置を用いることができる。特に、前記酸素ＰＳＡ装置は、効率よく低純度酸素を発生させることができるので、低純度酸素発生部２０として最適である。
【００１３】
上記低純度酸素発生部２０で発生して低純度酸素導出管２１に導出した低純度酸素は、必要に応じて設けられる酸素ブロワー２２で若干昇圧された後、弁２３を経て前記原料空気圧縮機１２の大気空気吸入側に設けられる原料空気吸入管１６に導入され、原料空気に添加混合され、酸素分の多い原料空気を生成する。
【００１４】
前記低純度酸素の酸素濃度は任意であり、低純度酸素発生部２０で使用する装置によって異なるが、酸素ＰＳＡ装置の場合は、その効率等を考慮すると、酸素濃度が８０〜９５体積％の低純度酸素であることが好ましい。一方、この低純度酸素と混合した後の酸素分の多い原料空気の酸素濃度は、安全性を考慮すると、高炉吹込用の送風機の実績等から、３０体積％以下、好ましくは２５体積％以下とすべきである。したがって、原料空気への低純度酸素の添加混合量は、原料空気量、低純度酸素の酸素濃度によって最適な量が決定されるので、これに見合った能力の装置を低純度酸素発生部２０で使用すればよい。
【００１５】
このように、原料空気に低純度酸素を添加混合して酸素分の多い原料空気とし，これを圧縮，冷却して液化精留を行うことにより、通常の大気空気を使用したときに比べて空気液化分離部１０から採取する酸素量を増量することができる。また、酸素ＰＳＡ装置等は、運転・停止を容易に行うことができるので、酸素需要の変動にも短時間で対応することが可能であり、酸素ＰＳＡ装置等自体も、酸素需要の変動に応じて増量運転や減量運転を行うことにより、経済的かつ効果的に製品酸素量の増減を行うことができる。
【００１６】
また、装置構成としては、通常の空気液化分離装置に前記酸素ＰＳＡ装置等を付設するとともに、その低純度酸素導出管２１を、原料空気圧縮機の原料空気吸入管１６等に連結するだけでよいため、新設の装置だけでなく、既存の装置へも対応が可能である。さらに、低純度酸素導出管２１の連結箇所は、原料空気圧縮機１２の大気空気吸入側で任意に選定することができるので、装置の設置状況等に応じて、原料空気圧縮機の原料空気吸入管２１だけでなく、空気フィルター１１を形成する吸入フィルターボックス等にも連結することができ、既存設備の改造も簡単に行うこができる。また、低純度酸素の発生圧力が、吸入原料空気への添加混合に十分な圧力を有している場合は、酸素ブロワー２２を省略することができる。
【００１７】
なお、空気液化分離部１０の構成は、少なくとも酸素を製品として採取できれば任意であり、本形態例に示すように窒素を同時に採取してもよく、アルゴン等を同時に採取するようにしてもよい。
【００１８】
【実施例】
図１に示す装置構成において、低純度酸素発生部２０として酸素ＰＳＡ装置を使用し、通常の定格運転時（運転１）と、酸素ＰＳＡ装置から９３体積％の低純度酸素を５００Ｎｍ３／ｈ添加混合した場合（運転２）と、７５０Ｎｍ３／ｈ添加混合した場合（運転３）とにおける製品酸素の採取量及び主要部（図１にＡ，Ｂ，Ｃ，Ｄ，Ｅで示すポイント）の流量（Ｎｍ３／ｈ）や組成（体積％）を以下に示す。なお、大気空気の酸素濃度は２０．９５体積％、製品酸素の純度は９９．６体積％、製品窒素の酸素含有量は１ｐｐｍ以下である。また、各運転における原料空気中の酸素濃度は、原料空気圧縮機の安全性を考慮して２３体積％以下とした。
【００１９】

Figure 0004150102
【００２０】
増量した分の酸素の電力原単位は、酸素ＰＳＡ装置の電力原単位が、０．３２ＫＷｈ／９３％Ｏ２−Ｎｍ３であるから、運転２において、５００×０．３２／３６０＝０．４４４ＫＷｈ／Ｎｍ３であった。これは、空気液化分離装置の電力原単位に遜色ないものである。
【００２１】
【発明の効果】
以上説明したように、本発明によれば、製品酸素の需要変動に容易に対応することができ、しかも、一般的な空気液化分離装置に簡単な設備を追加するだけで実施することができるので、新設の設備だけでなく、既存の設備にも容易に対応できる。さらに、低純度の酸素を発生する装置として酸素ＰＳＡ装置を用いることにより、ＰＳＡの特徴である起動停止の容易さから、酸素需要に応じた無駄のない運転ができる。
【図面の簡単な説明】
【図１】 本発明の空気液化分離装置の一形態例を示す概略系統図である。
【符号の説明】
１０…空気液化分離部、１１…空気フィルター、１２…原料空気圧縮機、１３…コールドボックス、１６…原料空気吸入管、２０…低純度酸素発生部、２１…低純度酸素導出管、２２…酸素ブロワー[0001]
BACKGROUND OF THE INVENTION
The present invention relates to an air liquefaction separation method and apparatus, and more particularly, to an air liquefaction separation method and apparatus that can increase or decrease the amount of oxygen produced according to fluctuations in demand for product oxygen.
[0002]
[Prior art and problems to be solved by the invention]
In an ordinary air liquefaction / separation apparatus, when the oxygen demand increases at a frequency of 1/2 or less, or 1/3 or less of the operation time of the apparatus, if the capacity of the apparatus is manufactured to the peak value, average production The operation state at the time of quantity is a weight reduction operation for the apparatus. Furthermore, when the oxygen demand is equal to or less than the average value, the operation is performed in a larger reduction region, so that the production efficiency is deteriorated, and as a result, the operation is inefficient in terms of power consumption. In general, when considering the weight reduction limit of the air compressor and the rectification tower in the air liquefaction separation apparatus, the production amount of the minimum weight reduction operation with respect to the rated production amount is about 75%.
[0003]
On the other hand, in the steel and chemical industries that use large amounts of oxygen gas, large-scale air liquefaction separators are installed to supply oxygen gas. The demand for oxygen gas depends on the operation plan, operation status, day of the week, and time. It varies greatly depending on the belt. For this reason, when demand decreases, a part of the product oxygen gas (excess) is liquefied and stored by heat exchange with liquefied nitrogen or the like, and when the demand increases, the stored liquefied oxygen is vaporized and supplied. May be installed. However, it is necessary to design such a special device corresponding to this in advance or to make extensive modifications to existing equipment, which causes a big problem in terms of equipment cost.
[0004]
Therefore, an object of the present invention is to provide an air liquefaction separation method and apparatus that can increase the amount of oxygen produced by simply adding a simple facility to a normal air liquefaction separation apparatus.
[0005]
[Means for Solving the Problems]
In order to achieve the above object, the air liquefaction separation method of the present invention is an air liquefaction separation method for compressing, cooling, liquefying and rectifying raw material air to obtain its component gas. By adding the low-purity oxygen generated by the attached low-purity oxygen generator to the atmospheric air to be sucked into the raw material air containing a large amount of oxygen, and compressing and cooling it to perform liquefaction rectification , At least oxygen is obtained as a product.
[0006]
Furthermore, the air liquefaction separation method of the present invention is such that the oxygen concentration of the raw material air rich in oxygen is not less than the oxygen concentration in the atmosphere and not more than 30% by volume, and the low-purity oxygen is a pressure fluctuation adsorption separation type. The pressure fluctuation adsorption separation type oxygen generator is operated in accordance with the low purity oxygen produced by an oxygen generator and having an oxygen concentration of 80 to 95% by volume and the fluctuation of the demand amount of oxygen obtained as the product. The supply amount of low-purity oxygen added to and mixed with the atmospheric air is adjusted by increasing operation, decreasing operation, or stopping operation.
[0007]
The air liquefaction separation apparatus of the present invention includes a raw material air compressor that compresses raw air composed of atmospheric air, an adsorber that purifies the compressed air compressed by the compressor, and a compression that is purified by the adsorber. A heat exchanger for cooling the purified air; and a rectifying tower for liquefying and rectifying the compressed purified cooling air cooled by the heat exchanger. In the air liquefaction rectification separation apparatus collected as a product, an apparatus for generating low-purity oxygen is attached, and a lead-out pipe for deriving the low-purity oxygen generated by the apparatus is provided for the intake of atmospheric air from the raw material air compressor It is connected to the side (inhalation system).
[0008]
Further, in the air liquefaction separation apparatus according to the present invention, the apparatus for generating low purity oxygen is a pressure fluctuation adsorption separation type oxygen generation apparatus, and the low purity oxygen derived from the pressure fluctuation adsorption separation type oxygen generation apparatus. Or a lead-out pipe for deriving low-purity oxygen without using a means for boosting low-purity oxygen. And a lead-out pipe for deriving low-purity oxygen from the pressure fluctuation adsorption separation-type oxygen generator is connected to an air-air suction filter box or a raw-material air suction pipe sucked by the raw-air compressor. It is characterized by being connected.
[0009]
DETAILED DESCRIPTION OF THE INVENTION
FIG. 1 is a schematic system diagram showing an embodiment of the air liquefaction separation apparatus of the present invention. This air liquefaction / separation apparatus collects oxygen and nitrogen as products. The air liquefaction / separation unit 10 has the same configuration as that of a normal air liquefaction / separation apparatus, and low purity oxygen is supplied to the air liquefaction / separation part 10. And a low-purity oxygen generator 20 to be supplied.
[0010]
In normal operation in the air liquefaction separation unit 10, atmospheric air (raw material air) sucked from the air filter 11 is compressed to a predetermined pressure by the raw material air compressor 12, and the compressed compressed air is introduced into an adsorber (not shown) for purification. After that, this compressed purified air is introduced into the cold box 13 and cooled, liquefied, and rectified, whereby product oxygen is collected from the path 14, and product nitrogen is collected from the path 15, and the product compressors 14a and 15a are used. Pumped.
[0011]
The cold box 13 is provided with known devices such as a heat exchanger, a rectification column, a condenser, and an expansion turbine, and nitrogen and oxygen, which are atmospheric component gases, are obtained by a known cryogenic separation method. To be separated.
[0012]
As the low-purity oxygen generation unit 20, various types can be used as long as they can generate low-purity oxygen containing oxygen at a higher concentration than atmospheric air. For example, pressure fluctuation adsorption called an oxygen PSA device can be used. A device that generates low-purity oxygen using atmospheric air as a raw material, such as a separation-type oxygen generator or a membrane-type oxygen concentrator, can be used. In particular, the oxygen PSA apparatus can generate low-purity oxygen efficiently, and is optimal as the low-purity oxygen generation unit 20.
[0013]
The low-purity oxygen generated in the low-purity oxygen generator 20 and led to the low-purity oxygen outlet pipe 21 is slightly boosted by an oxygen blower 22 provided as necessary, and then passes through the valve 23 to the raw air compressor. 12 is introduced into a raw material air suction pipe 16 provided on the atmospheric air suction side, and added to and mixed with the raw material air to generate raw material air containing a large amount of oxygen.
[0014]
The oxygen concentration of the low-purity oxygen is arbitrary, and varies depending on the device used in the low-purity oxygen generator 20, but in the case of an oxygen PSA device, the oxygen concentration is a low value of 80 to 95% by volume in consideration of its efficiency and the like. Preferably it is pure oxygen. On the other hand, the oxygen concentration of the raw material air containing a large amount of oxygen after mixing with this low-purity oxygen is 30% by volume or less, preferably 25% by volume or less, in consideration of safety, from the results of the blower for blast furnace blowing. Should. Therefore, the amount of the low purity oxygen added to the raw air is determined by the amount of the raw air and the oxygen concentration of the low purity oxygen. Use it.
[0015]
In this way, raw material air is mixed with low-purity oxygen to form a raw material air containing a large amount of oxygen, and this is compressed and cooled to perform liquefaction rectification, so that air is used compared to when normal atmospheric air is used. The amount of oxygen collected from the liquefaction separation unit 10 can be increased. In addition, since the oxygen PSA device and the like can be easily operated and stopped, it is possible to cope with fluctuations in oxygen demand in a short time, and the oxygen PSA device itself also responds to fluctuations in oxygen demand. By performing the increase operation and the decrease operation, the amount of product oxygen can be increased and decreased economically and effectively.
[0016]
As an apparatus configuration, the oxygen PSA apparatus and the like are attached to a normal air liquefaction separation apparatus, and the low-purity oxygen outlet pipe 21 only needs to be connected to the raw air intake pipe 16 of the raw air compressor. Therefore, it is possible to deal with not only newly installed devices but also existing devices. Furthermore, the connection location of the low-purity oxygen outlet pipe 21 can be arbitrarily selected on the atmospheric air suction side of the raw material air compressor 12, so that the raw material air intake of the raw material air compressor according to the installation status of the apparatus, etc. It can be connected not only to the pipe 21 but also to a suction filter box or the like forming the air filter 11, and the existing equipment can be easily modified. Moreover, when the generation pressure of low-purity oxygen has sufficient pressure for addition and mixing with the intake raw material air, the oxygen blower 22 can be omitted.
[0017]
The configuration of the air liquefaction separation unit 10 is arbitrary as long as at least oxygen can be collected as a product. Nitrogen may be collected simultaneously as shown in this embodiment, or argon or the like may be collected simultaneously.
[0018]
【Example】
In the apparatus configuration shown in FIG. 1, an oxygen PSA apparatus is used as the low-purity oxygen generation unit 20, and during normal rated operation (operation 1), 500 Nm 3 / h of 93% by volume of low-purity oxygen is added from the oxygen PSA apparatus. when mixed with (operation 2), the flow rate when mixed 750 Nm 3 / h added collection amount and the main portion of the oxygen product in (operation 3) and (point shown in FIG. 1 a, B, C, D, with E) (Nm 3 / h) and composition (volume%) are shown below. The oxygen concentration of atmospheric air is 20.95% by volume, the purity of product oxygen is 99.6% by volume, and the oxygen content of product nitrogen is 1 ppm or less. Further, the oxygen concentration in the raw material air in each operation was set to 23% by volume or less in consideration of the safety of the raw material air compressor.
[0019]
Figure 0004150102
[0020]
Since the power unit of oxygen increased is 0.32 kWh / 93% O 2 —Nm 3 in the oxygen PSA device, 500 × 0.32 / 360 = 0.444 kWh in operation 2 It was / Nm 3. This is comparable to the power unit of the air liquefaction separation device.
[0021]
【The invention's effect】
As described above, according to the present invention, it is possible to easily cope with fluctuations in the demand for product oxygen, and furthermore, it can be carried out simply by adding simple equipment to a general air liquefaction separation apparatus. It can easily accommodate not only new equipment but also existing equipment. Furthermore, by using an oxygen PSA device as a device for generating low-purity oxygen, it is possible to operate without waste according to the demand for oxygen because of the ease of starting and stopping, which is a feature of PSA.
[Brief description of the drawings]
FIG. 1 is a schematic system diagram showing an embodiment of an air liquefaction separation apparatus according to the present invention.
[Explanation of symbols]
DESCRIPTION OF SYMBOLS 10 ... Air liquefaction separation part, 11 ... Air filter, 12 ... Raw material air compressor, 13 ... Cold box, 16 ... Raw material air suction pipe, 20 ... Low-purity oxygen generation part, 21 ... Low-purity oxygen lead-out pipe, 22 ... Oxygen Blower

Claims (9)

原料空気を圧縮・冷却・液化・精留してその成分ガスを得る空気液化分離方法において，原料空気を圧縮する原料空気圧縮機が吸入する大気空気に、付設した低純度の酸素を発生する装置で発生した低純度の酸素を添加混合して酸素分の多い原料空気とし，これを圧縮，冷却して液化精留を行うことにより、少なくとも酸素を製品として得ることを特徴とする空気液化分離方法。In an air liquefaction separation method that obtains component gases by compressing, cooling, liquefying and rectifying raw material air, a device for generating low-purity oxygen attached to the atmospheric air sucked by the raw air compressor that compresses the raw air The air liquefaction separation method is characterized in that at least oxygen is obtained as a product by adding and mixing the low purity oxygen generated in the process to make a raw material air rich in oxygen, compressing and cooling it to perform liquefaction rectification . 前記酸素分の多い原料空気の酸素濃度を、大気の酸素濃度以上で、３０体積％以下とすることを特徴とする請求項１記載の空気液化分離方法。2. The air liquefaction separation method according to claim 1, wherein the oxygen concentration of the raw material air rich in oxygen is not less than the oxygen concentration in the atmosphere and not more than 30% by volume. 前記低純度の酸素が、圧力変動吸着分離式酸素発生装置により製造され、その酸素濃度が８０〜９５体積％の低純度酸素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。2. The air liquefaction separation method according to claim 1, wherein the low-purity oxygen is produced by a pressure fluctuation adsorption separation type oxygen generator, and the oxygen concentration is low-purity oxygen of 80 to 95% by volume. 前記製品として得る酸素の需要量の変動に応じて，前記圧力変動吸着分離式酸素発生装置の運転を増量運転，減量運転又は運転停止することにより、前記大気空気に添加混合する低純度酸素の供給量を調節することを特徴とする請求項３記載の空気液化分離方法。Supplying low-purity oxygen to be added to and mixed with the atmospheric air by increasing, decreasing, or stopping the operation of the pressure fluctuation adsorption separation type oxygen generator according to fluctuations in the amount of oxygen demand obtained as the product The air liquefaction separation method according to claim 3, wherein the amount is adjusted. 大気空気からなる原料空気を圧縮する原料空気圧縮機と、該圧縮機で圧縮された圧縮空気を精製する吸着器と、該吸着器で精製された圧縮精製空気を冷却する熱交換器と、該熱交換器で冷却された圧縮精製冷却空気を液化・精留する精留塔を備え、前記原料空気の成分ガスを液化精留分離し、少なくとも酸素を製品として採取する空気液化精留分離装置において、低純度の酸素を発生する装置を付設するとともに、該装置で発生した低純度の酸素を導出する導出管を、前記原料空気圧縮機の大気空気吸入側に連結したことを特徴とする空気液化分離装置。A raw material air compressor that compresses raw air consisting of atmospheric air, an adsorber that purifies the compressed air compressed by the compressor, a heat exchanger that cools the compressed purified air purified by the adsorber, and In an air liquefaction rectification separation apparatus comprising a rectification tower for liquefying and rectifying compressed and purified cooling air cooled by a heat exchanger, liquefying and separating component gases of the raw material air, and collecting at least oxygen as a product An air liquefaction characterized in that an apparatus for generating low-purity oxygen is attached, and a lead-out pipe for deriving the low-purity oxygen generated in the apparatus is connected to the atmospheric air intake side of the raw material air compressor Separation device. 前記低純度の酸素を発生する装置が，圧力変動吸着分離式酸素発生装置であることを特徴とする請求項５記載の空気液化分離装置。6. The air liquefaction separation apparatus according to claim 5, wherein the apparatus for generating low-purity oxygen is a pressure fluctuation adsorption separation type oxygen generation apparatus. 前記圧力変動吸着分離式酸素発生装置から導出される低純度の酸素を昇圧するための酸素ブロワーを備えていることを特徴とする請求項６記載の空気液化分離装置。The air liquefaction separation apparatus according to claim 6, further comprising an oxygen blower for boosting low-purity oxygen derived from the pressure fluctuation adsorption separation type oxygen generator. 前記圧力変動吸着分離式酸素発生装置から導出される低純度の酸素を昇圧する手段を介さずに、前記低純度の酸素を導出する導出管を前記原料空気圧縮機の大気空気吸入側に連結したことを特徴とする請求項６記載の空気液化分離装置。A lead-out pipe for leading out the low-purity oxygen was connected to the atmospheric air suction side of the raw material air compressor without using a means for increasing the pressure of the low-purity oxygen derived from the pressure fluctuation adsorption separation type oxygen generator. The air liquefaction separation apparatus according to claim 6. 前記圧力変動吸着分離式酸素発生装置から低純度の酸素を導出する導出管を、前記原料空気圧縮機が吸入する大気空気の吸入フィルターボックス又は原料空気吸入管に連結したことを特徴とする請求項６記載の空気液化分離装置。The outlet pipe for extracting low-purity oxygen from the pressure fluctuation adsorption separation type oxygen generator is connected to a suction filter box for atmospheric air sucked by the raw air compressor or a raw air suction pipe. 6. The air liquefaction separation apparatus according to 6.
JP13887598A 1998-05-20 1998-05-20 Air liquefaction separation method and apparatus Expired - Fee Related JP4150102B2 (en)

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