JP2009052807A - Low-temperature air liquefaction separation device and its operation method - Google Patents

Low-temperature air liquefaction separation device and its operation method Download PDF

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JP2009052807A
JP2009052807A JP2007220015A JP2007220015A JP2009052807A JP 2009052807 A JP2009052807 A JP 2009052807A JP 2007220015 A JP2007220015 A JP 2007220015A JP 2007220015 A JP2007220015 A JP 2007220015A JP 2009052807 A JP2009052807 A JP 2009052807A
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air
heat exchanger
raw material
production operation
material air
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JP4594360B2 (en
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Hitoshi Asaoka
斉 浅岡
Tamotsu Hashimoto
保 橋本
Takashi Oyama
隆司 大山
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SHINKO AIR WATER CRYOPLANT Ltd
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SHINKO AIR WATER CRYOPLANT Ltd
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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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—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
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air

Abstract

<P>PROBLEM TO BE SOLVED: To provide a low-temperature air liquefaction separation device capable of switching a gas manufacturing operation for manufacturing nitrogen or oxygen gas and the like to a liquid manufacturing operation for manufacturing liquid nitrogen or oxygen and the like in a short time without heating an oil and a bearing of a turbine and performing a recooling operation of a heat exchanger. <P>SOLUTION: A liquefaction heat exchanger 7 is constituted to be operated in both of a gas manufacturing operation and a liquid manufacturing operation, so that, in the gas manufacturing operation, a part of the refined material air is introduced to a lower tower 15b of a duplex refining tower 15 through a main heat exchanger 4, and the remaining material air is introduced to the same through a liquefaction heat exchanger 7, and in the liquid manufacturing operation, a part of the refined material air is introduced to the lower tower 15b of the duplex refining tower 15 through the main heat exchanger 4, a part of the remaining material air is compressed by a pressure-raising compressor 9b and introduced to the same through the liquefaction heat exchanger 7, and further the remaining of a part of the remaining is compressed by a compressor 12a of the high-pressure expansion turbine 12, expanded by the liquefaction heat exchanger 7 and an expander 12b of the high-pressure expansion turbine 12, and introduced to the same as the cold.operation. <P>COPYRIGHT: (C)2009,JPO&INPIT

Description

本発明は、深冷空気液化分離装置およびその運転方法に係り、より詳しくは、窒素、酸素ガス等を製造するガス製造運転から液体窒素、酸素等を製造する液製造運転に切換えるに際して、液化熱交換器の再冷却運転を行う必要がなく、切換え開始後短時間のうちに液製造運転に移行することを可能ならしめる深冷空気液化分離装置およびその運転方法に関するものである。   The present invention relates to a cryogenic air liquefaction separation apparatus and an operation method thereof, and more specifically, when switching from a gas production operation for producing nitrogen, oxygen gas or the like to a liquid production operation for producing liquid nitrogen, oxygen or the like, The present invention relates to a chilled air liquefaction separation apparatus and a method for operating the same, which makes it possible to shift to a liquid production operation in a short time after the start of switching without performing a recooling operation of the exchanger.

鉄鋼業等の酸素や窒素を大量に消費する工業分野においては、酸素や窒素の供給源として深冷空気液化分離装置が使用されている。このような深冷空気液化分離装置の中に、電力コストが高い昼間には窒素、酸素ガス等を製造するガス製造運転を行う一方、電力コストが安い夜間になると切換えて、液体窒素、酸素等を製造する液製造運転に移行できるようにした深冷空気液化分離装置がある。   In the industrial field that consumes a large amount of oxygen and nitrogen such as in the steel industry, a cryogenic air liquefaction separation apparatus is used as a supply source of oxygen and nitrogen. In such a cryogenic air liquefaction separation device, gas production operation to produce nitrogen, oxygen gas, etc. is performed during the daytime when the power cost is high, while switching to liquid nitrogen, oxygen, etc. at night when the power cost is low There is a chilled air liquefaction separation device that can be shifted to a liquid production operation for producing a liquid.

以下、従来例に係る一般的な液化装置付きの深冷空気液化分離装置を、その系統図の図５を参照しながら説明する。即ち、一般的な液化装置付きの深冷空気液化分離装置は、空気ろ過器５１から吸込まれ、原料空気圧縮機５２で圧縮されると共に、水洗冷却塔５３で冷却された原料空気と、精留塔５５から出た製品窒素と製品酸素とを熱交換させる熱交換器（以下、主熱交換器という）５４と、液化装置６３とを備えている。この液化装置６３は、前記精留塔５５から出て主熱交換器５４で常温に戻された製品窒素の一部を昇圧するための循環窒素圧縮機６２、昇圧された窒素を液化するための熱交換器６７、前記精留塔５５から出て主熱交換器５４で常温に戻されると共に、酸素圧縮機６１で圧縮された製品酸素の一部を液化するための熱交換器７７、寒冷を発生するための膨張タービン７２，７３等から構成されている。   Hereinafter, a general cold air liquefaction separation apparatus with a liquefaction apparatus according to a conventional example will be described with reference to FIG. That is, a general cryogenic air liquefaction separation apparatus with a liquefier is sucked from an air filter 51, compressed by a raw air compressor 52, and cooled by a water-washing cooling tower 53, and rectification. A heat exchanger (hereinafter referred to as a main heat exchanger) 54 for exchanging heat between product nitrogen and product oxygen discharged from the tower 55 and a liquefaction device 63 are provided. The liquefying device 63 is a circulating nitrogen compressor 62 for boosting a part of product nitrogen that has come out of the rectification column 55 and returned to room temperature by the main heat exchanger 54, and for liquefying the boosted nitrogen. A heat exchanger 67 and a heat exchanger 77 for liquefying part of product oxygen compressed by the oxygen compressor 61 and cooled to normal temperature by the main heat exchanger 54 after exiting from the rectifying column 55 It is comprised from the expansion turbines 72 and 73 etc. for generating.

このような液化装置付きの深冷空気液化分離装置は、精留塔５５から主熱交換器５４を通って排出されるガス酸素、ガス窒素の一部を、液化装置６３を起動することによって液化して、液体酸素と、液体窒素を製造している。液化装置６３の起動とは、循環窒素圧縮機６２、膨張タービン７２，７３の起動、および熱交換器６７，７７における熱交換の開始を意味する。この特性を利用して、電力コストが安い夜間は循環窒素圧縮機６２を起動してガス酸素、ガス窒素の一部を液化備蓄し、電力コストが高い昼間は循環窒素圧縮機６２の運転を停止してガス製品のみを製造する運転を行っている。また、熱交換器６７，７７は、液化装置６３が運転されていない昼間では、次の運転のために低温状態に保持された待機状態になっている。   Such a chilled air liquefaction separation apparatus with a liquefaction device liquefies a part of gaseous oxygen and gaseous nitrogen discharged from the rectification column 55 through the main heat exchanger 54 by activating the liquefier 63. Liquid oxygen and liquid nitrogen are produced. The activation of the liquefaction device 63 means the activation of the circulating nitrogen compressor 62 and the expansion turbines 72 and 73 and the start of heat exchange in the heat exchangers 67 and 77. Utilizing this characteristic, the circulating nitrogen compressor 62 is started at night when the power cost is low to store a part of gaseous oxygen and gaseous nitrogen, and the circulating nitrogen compressor 62 is stopped during the day when the power cost is high. The company operates to produce only gas products. Further, the heat exchangers 67 and 77 are in a standby state in which the liquefying device 63 is kept in a low temperature state for the next operation during the daytime when the liquefying device 63 is not operated.

ところで、液化装置６３の膨張タービン７２，７３にオイルベアリング式の軸受が使用されている場合には、運転中は軸受の温度上昇を防止するために、軸受用のオイルを軸受とオイルクーラーとの間で循環させて軸受の温度上昇を防止している。また、液化装置６３の運転停止中においても、オイルが固化したりしないように軸受用のオイルを軸受とオイルクーラーとの間で循環させて軸受の温度低下を防止するようにしている。ところが、膨張タービン７２，７３の運転停止中においても液化装置６３が低温状態に保持されているため、特に冷却水の温度が低い冬季では、軸受の温度が次第に低下し、これに伴ってオイルの温度も相当低下する。この状態で運転すると、軸受にかじりが生じたり、振動が発生したりするため、膨張タービン７２や７３を起動するに際して、オイルや軸受を所定の温度になるまで加温する必要がある。   By the way, when oil bearing type bearings are used for the expansion turbines 72 and 73 of the liquefying device 63, the oil for the bearing is used for the bearing and the oil cooler in order to prevent the temperature of the bearing from rising during operation. Circulating between them prevents the bearing temperature from rising. Further, even when the operation of the liquefying device 63 is stopped, the bearing oil is circulated between the bearing and the oil cooler so that the oil does not solidify to prevent the temperature of the bearing from decreasing. However, since the liquefaction device 63 is kept at a low temperature even when the operation of the expansion turbines 72 and 73 is stopped, the temperature of the bearing gradually decreases, especially in the winter when the temperature of the cooling water is low. The temperature also drops considerably. When the operation is performed in this state, the bearings are galling or vibrations are generated. Therefore, when the expansion turbines 72 and 73 are started, it is necessary to heat the oil and the bearings to a predetermined temperature.

そのため、液化装置６３の膨張タービン７２，７３を起動する際には、予め低負荷状態による暖気運転を行い、オイルや軸受が所定の温度になるまで加温していた。この暖気運転の所要時間は、冷却水の温度、停止時間、あるいはタービンの大きさ等により相違するが、１時間かかることもあるため、ガスの液化ができないのに加えて、循環窒素圧縮機の運転に要する電力が無駄になるという問題があった。そこで、水洗冷却塔から導出される加温された約５０℃の温排水をオイルクーラーに導入してオイルを約３０℃に加温し、加温したオイルを軸受けに導入して軸受を加温した後に、膨張タービン７２，７３を起動するようにしている。この場合、温排水を利用するため、初期設備コストを要するものの、ランニングコストがほとんど掛からないという利点がある。また、これにより、膨張タービン７２，７３の起動に要する所要時間を大幅に短縮できると記載されている（例えば、特許文献１参照）。
特開平１０−２９２９８６号公報 Therefore, when starting up the expansion turbines 72 and 73 of the liquefying device 63, a warm-up operation in a low-load state is performed in advance, and the oil and the bearing are heated up to a predetermined temperature. The time required for this warm-up operation varies depending on the temperature of the cooling water, the stop time, or the size of the turbine, but it may take one hour. In addition to the fact that the gas cannot be liquefied, the circulating nitrogen compressor There was a problem that the electric power required for operation was wasted. Therefore, warmed water drained from the water cooling tower is heated to about 50 ° C and introduced into the oil cooler to heat the oil to about 30 ° C. The heated oil is introduced into the bearing to heat the bearing. After that, the expansion turbines 72 and 73 are started. In this case, since warm waste water is used, the initial equipment cost is required, but there is an advantage that almost no running cost is required. Further, it is described that the time required for starting the expansion turbines 72 and 73 can be greatly shortened (see, for example, Patent Document 1).
JP-A-10-292986

上記従来例に係る液化装置付きの深冷空気液化分離装置によれば、タービンの起動時間の短縮により、ガス製造運転から液製造運転への移行時間が短縮されるため、それなりに優れていると考えられる。しかしながら、この従来例に係る液化装置付きの深冷空気液化分離装置には後述するような解決すべき課題がある。   According to the cryogenic air liquefaction separation apparatus with a liquefier according to the above conventional example, the transition time from the gas production operation to the liquid production operation is shortened by shortening the startup time of the turbine. Conceivable. However, the cryogenic air liquefaction separation apparatus with a liquefier according to this conventional example has problems to be solved as described later.

上記従来例に係る液化装置付きの深冷空気液化分離装置では、運転停止中の液化装置は低温状態に保持される。しかしながら、外部からの入熱を完全に遮断することはほぼ不可能であり、１０〜１４時間に及ぶ昼間の運転停止中に、外部からの入熱により熱交換器の温度が数十℃は上昇する。また、熱交換器内での熱伝導により、通常運転時は常温である温端側が、運転停止中にマイナス数十℃に冷却される。   In the chilled air liquefaction separation apparatus with a liquefier according to the above-described conventional example, the liquefier that is not operating is kept in a low temperature state. However, it is almost impossible to completely shut off the heat input from the outside, and the heat exchanger temperature increases by several tens of degrees Celsius due to heat input from the outside during the daytime shutdown for 10 to 14 hours. To do. Also, due to heat conduction in the heat exchanger, the warm end side, which is normal temperature during normal operation, is cooled to minus several tens of degrees Celsius during operation stop.

このような状態で、液化装置が起動されるため、起動直後は低温流体が低温のまま放出され、常温ラインの配管が破損する可能性があるという問題、運転停止中における入熱により昇温した熱交換器を再冷却しなければならないという問題、および運転停止中における入熱による熱交換器の膨張と収縮の繰り返し、つまり熱ひずみの繰り返しにより熱交換器が疲労破損し、メンテナンスコストが嵩むという問題が残っている。前記熱交換器の再冷却所要時間は、季節、この液化装置の停止時間、熱交換器の大きさ（容量）等によって相違するが、およそ０．５から１．０時間である。従って、およそ０．５から１．０時間の熱交換器の再冷却運転中は液体窒素、酸素等を製造することができないから、好ましくない。   In such a state, since the liquefaction device is started, immediately after startup, the low temperature fluid is discharged at a low temperature, and there is a possibility that the piping of the normal temperature line may be damaged. The problem of having to re-cool the heat exchanger, and repeated heat expansion and contraction of the heat exchanger due to heat input during shutdown, that is, the heat exchanger fatigues due to repeated thermal strain, increasing maintenance costs The problem remains. The time required for recooling the heat exchanger is approximately 0.5 to 1.0 hour, although it varies depending on the season, the stop time of the liquefier, the size (capacity) of the heat exchanger, and the like. Accordingly, liquid nitrogen, oxygen, etc. cannot be produced during the recooling operation of the heat exchanger for about 0.5 to 1.0 hour, which is not preferable.

従って、本発明の目的は、窒素、酸素ガス等を製造するガス製造運転から液体窒素、酸素等を製造する液製造運転に切換えるに際して、熱交換器の再冷却運転を行う必要がなく、切換え時に低温流体が低温のまま常温ラインに放出されることもなく、熱交換器に繰り返し応力を与えることもなく、短時間のうちに液製造運転に移行することを可能ならしめる深冷空気液化分離装置およびその運転方法を提供することである。   Therefore, the object of the present invention is to eliminate the need for recooling operation of the heat exchanger when switching from the gas production operation for producing nitrogen, oxygen gas, etc. to the liquid production operation for producing liquid nitrogen, oxygen, etc. Cryogenic air liquefaction separation device that makes it possible to move to a liquid production operation in a short time without the low temperature fluid being discharged to the room temperature line at a low temperature and without repeatedly applying stress to the heat exchanger. And providing a method of operation thereof.

上記課題を解決するために、本発明の請求項１に係る深冷空気液化分離装置が採用した手段は、原料空気圧縮機と、この原料空気圧縮機で圧縮された原料空気を予冷する予冷ユニットと、この予冷ユニットで予冷された原料空気から水分・炭酸ガスを除去して精製する吸着塔ユニットと、この吸着塔ユニットで精製された原料空気の一部を冷却する主熱交換器と、前記吸着塔ユニットで精製された原料空気の残りを圧縮する昇圧圧縮機と、この昇圧圧縮機で昇圧された原料空気の一部を液化するための液化熱交換器と、前記昇圧圧縮機で圧縮された原料空気の残りの一部を膨張させて寒冷を発生させる高圧膨張タービンと、前記主熱交換器、液化熱交換器を経て導入された原料空気を窒素と酸素等に精留分離する複式精留塔と、これらに付随する付帯設備とを備えると共に、ガス製造運転と液製造運転とに切換え操作される深冷空気液化分離装置において、前記ガス製造運転中は開弁され、前記液製造運転中は閉弁される第１開閉弁が介装され、前記吸着塔ユニットで精製された原料空気の残りを前記液化熱交換器に導入する第１空気導入ラインと、前記ガス製造運転中は開弁され、前記液製造運転中は閉弁される第２開閉弁が介装され、前記液化熱交換器から出た原料空気を複式精留塔に導入する第２空気導入ラインと、前記ガス製造運転中は閉弁され、前記液製造運転中は開弁される第３開閉弁が介装され、前記高圧膨張タービンの圧縮機側から出た原料空気を前記液化熱交換器に導入する第３空気導入ラインと、前記ガス製造運転中は閉弁され、前記液製造運転中は開弁される第４開閉弁が介装され、前記液化熱交換器から出た原料空気を前記高圧膨張タービンの膨張機側に導入する第４空気導入ラインと、液製造運転に際して前記第４空気導入ラインから導入され、前記高圧膨張タービンの膨張機で膨張されて寒冷を発生した原料空気を複式精留塔に導入する第５空気導入ラインを備えたことを特徴とするものである。   In order to solve the above problems, the means adopted by the chilled air liquefaction separation apparatus according to claim 1 of the present invention includes a raw air compressor and a precooling unit for precooling the raw air compressed by the raw air compressor. An adsorption tower unit that removes moisture / carbon dioxide gas from the raw air precooled by the precooling unit, purifies the main heat exchanger that cools a part of the raw material air purified by the adsorption tower unit, A pressurizing compressor for compressing the remainder of the raw material air purified by the adsorption tower unit, a liquefied heat exchanger for liquefying a part of the raw air pressurized by the pressurizing compressor, and the pressurizing compressor A high-pressure expansion turbine that expands the remaining part of the raw material air to generate cold, and a double precision rectifier that separates the raw material air introduced through the main heat exchanger and the liquefied heat exchanger into nitrogen and oxygen. Towers and their accompanying A chilled air liquefaction separation device that is switched between a gas production operation and a liquid production operation, and is opened during the gas production operation and closed during the liquid production operation. A first air introduction line which is provided with one on-off valve and introduces the remainder of the raw material air purified by the adsorption tower unit to the liquefied heat exchanger, and is opened during the gas production operation, and the liquid production operation A second on-off valve that is closed inside is interposed, a second air introduction line that introduces raw air from the liquefied heat exchanger into the double rectification column, and is closed during the gas production operation, A third on-off valve that is opened during the liquid production operation is interposed, and a third air introduction line that introduces raw air that has come out from the compressor side of the high-pressure expansion turbine into the liquefied heat exchanger, and the gas The valve is closed during the manufacturing operation and is opened during the liquid manufacturing operation. A fourth open / close valve is interposed, and a fourth air introduction line for introducing the raw air discharged from the liquefied heat exchanger to the expander side of the high-pressure expansion turbine and a fourth air introduction line for the liquid production operation And a fifth air introduction line for introducing the raw material air, which has been expanded by the expander of the high-pressure expansion turbine and generates cold, into the double rectification column.

本発明の請求項２に係る深冷空気液化分離装置の運転方法が採用した手段は、原料空気を原料空気圧縮機で圧縮し、原料空気圧縮機から出た原料空気を予冷ユニットで予冷し、予冷した原料空気を水分・炭酸ガスを除去する吸着塔ユニットに導入し、この吸着塔ユニットから出た原料空気の一部を主熱交換器に導入し、残りの原料空気を液化熱交換器に導入すると共に、前記主熱交換器、および液化熱交換器から出た原料空気を複式精留塔に導入して窒素ガスと酸素ガス等を製造するガス製造運転と、前記吸着塔ユニットから出た原料空気の一部を主熱交換器に導入し、残りの原料空気を昇圧圧縮機で昇圧させた後に二分し、二分した一方の原料空気を液化熱交換器に導入し、二分した他方の原料空気を高圧膨張タービンの圧縮機で圧縮して液化熱交換器に導入し、この液化熱交換器から出た原料空気を高圧膨張タービンの膨張機で膨張させた後に複式精留塔に導入すると共に、前記主熱交換器から出た原料空気の一部、および前記液化熱交換器から出た二分した一方の原料空気を複式精留塔に導入して液体窒素と液体酸素等を製造する液製造運転とを自動切換することを特徴とするものである。   The means employed by the operation method of the chilled air liquefaction separation apparatus according to claim 2 of the present invention compresses the raw material air with the raw material air compressor, precools the raw material air discharged from the raw material air compressor with the precooling unit, The pre-cooled raw material air is introduced into the adsorption tower unit that removes moisture and carbon dioxide gas, a part of the raw air discharged from the adsorption tower unit is introduced into the main heat exchanger, and the remaining raw material air is converted into the liquefied heat exchanger. Gas production operation for introducing nitrogen gas, oxygen gas, etc. by introducing raw air from the main heat exchanger and the liquefied heat exchanger into the double rectification column, and from the adsorption tower unit A part of the raw material air is introduced into the main heat exchanger, and the remaining raw material air is boosted with a booster compressor and then divided into two parts. One of the two raw material airs is introduced into the liquefied heat exchanger and the other half of the raw material is divided into two parts. Compress the air with the compressor of the high-pressure expansion turbine The raw material air introduced into the liquefied heat exchanger and expanded from the liquefied heat exchanger with the expander of the high-pressure expansion turbine is introduced into the double rectification tower, and the raw material air discharged from the main heat exchanger A part and one of the bisected raw air discharged from the liquefied heat exchanger is introduced into a double rectification column to automatically switch between liquid production operations for producing liquid nitrogen, liquid oxygen, etc. It is.

本発明の請求項１に係る深冷空気液化分離装置、請求項２に係る深冷空気液化分離装置の運転方法では、深冷空気液化分離装置のガス製造運転においては、吸着塔ユニットで精製された原料空気の一部が主熱交換器に導入されると共に、主熱交換器から出た圧縮空気が複式精留塔に供給される。また、これと並行して、吸着塔ユニットで精製された原料空気の残りが第１空気導入ラインから液化熱交換器に導入され、この液化熱交換器から出た原料空気が第２空気導入ラインから複式精留塔に導入される。   In the operation method of the cryogenic air liquefaction separation apparatus according to claim 1 of the present invention and the cryogenic air liquefaction separation apparatus according to claim 2, the gas production operation of the cryogenic air liquefaction separation apparatus is purified by an adsorption tower unit. A part of the raw material air is introduced into the main heat exchanger, and compressed air from the main heat exchanger is supplied to the double rectification column. In parallel with this, the remainder of the raw material air purified by the adsorption tower unit is introduced into the liquefied heat exchanger from the first air introduction line, and the raw air discharged from the liquefied heat exchanger is introduced into the second air introduction line. To be introduced into the double rectification column.

一方、深冷空気液化分離装置の液製造運転においては、吸着塔ユニットで精製された原料空気の一部が主熱交換器に導入されると共に、この主熱交換器から出た圧縮空気が複式精留塔に供給される。また、これと並行して、昇圧圧縮機で圧縮された残りの原料空気の一部が液化熱交換器に導入され、この液化熱交換器を出た原料空気が複式精留塔に導入される。そして、昇圧圧縮機で圧縮された残りの原料空気の一部の残りが高圧膨張タービンの圧縮機側に導入され、この圧縮機側から出た原料空気が第３空気導入ラインから液化熱交換器に導入され、この液化熱交換器を出た原料空気が第４空気導入ラインから高圧膨張タービンの膨張機側に導入され、この高圧膨張タービンでの膨張により発生した寒冷が複式精留塔に導入される。   On the other hand, in the liquid manufacturing operation of the cryogenic air liquefaction separation apparatus, a part of the raw material air purified by the adsorption tower unit is introduced into the main heat exchanger, and the compressed air from the main heat exchanger is duplicated. Supplied to the rectification tower. In parallel with this, a part of the remaining raw material air compressed by the booster compressor is introduced into the liquefied heat exchanger, and the raw material air exiting this liquefied heat exchanger is introduced into the double rectification column. . A part of the remaining raw material air compressed by the booster compressor is introduced to the compressor side of the high-pressure expansion turbine, and the raw material air discharged from the compressor side is liquefied heat exchanger from the third air introduction line. The raw material air that has been introduced into the liquefied heat exchanger and introduced from the fourth air introduction line is introduced into the expander side of the high-pressure expansion turbine, and the cold generated by the expansion in the high-pressure expansion turbine is introduced into the double rectification column. Is done.

本発明の請求項１に係る深冷空気液化分離装置、請求項２に係る深冷空気液化分離装置の運転方法では、上記のとおり、ガス製造運転と液製造運転とが交互に繰り返されるのであるが、液化熱交換器は液製造運転中のみならず、ガス製造運転中も作動されるように構成されている。従って、本発明の請求項１に係る深冷空気液化分離装置、請求項２に係る深冷空気液化分離装置の運転方法によれば、下記のとおりの効果を得ることができる。   In the operation method of the cryogenic air liquefaction separation apparatus according to claim 1 of the present invention and the cryogenic air liquefaction separation apparatus according to claim 2, the gas production operation and the liquid production operation are alternately repeated as described above. However, the liquefied heat exchanger is configured to be operated not only during the liquid production operation but also during the gas production operation. Therefore, according to the operation method of the chilled air liquefaction separation apparatus according to claim 1 of the present invention and the chilled air liquefaction separation apparatus according to claim 2, the following effects can be obtained.

（１）ガス製造運転中の液化熱交換器のガス出入り口間の温度分布は、液製造運転中における温度分布とほぼ同等に保持されていて、ガス製造運転から液製造運転に切換えるに際して冷却運転をする必要がないため、極めて短時間のうちにガス製造運転中の深冷空気液化分離装置を液製造運転に移行させることができる。これにより、実質的な液製造運転時間が増加し、液体酸素・窒素等の生産性が向上するため、それら液体酸素・窒素等のコスト低減に大いに寄与することができる。
（２）ガス製造運転中の液化熱交換器のガス出入り口間の温度分布は、液製造運転中における温度分布とほぼ同等に保持されている。従って、温端側がマイナスの温度になっているということがなく、液製造運転への切換え時に低温流体が低温のまま放出されることがないため、常温ラインの配管が損傷するという危険性がない。
（３）液化熱交換器は収縮と膨張とを繰り返すことがないため、液化熱交換器の耐久寿命が向上する。 (1) The temperature distribution between the gas inlet and outlet of the liquefied heat exchanger during the gas production operation is maintained almost equal to the temperature distribution during the liquid production operation, and the cooling operation is performed when switching from the gas production operation to the liquid production operation. Therefore, the chilled air liquefaction separation apparatus during the gas production operation can be shifted to the liquid production operation in a very short time. Thereby, substantial liquid manufacturing operation time increases and productivity of liquid oxygen, nitrogen, etc. improves, Therefore It can contribute greatly to the cost reduction of these liquid oxygen, nitrogen, etc.
(2) The temperature distribution between the gas inlets and outlets of the liquefied heat exchanger during the gas production operation is maintained substantially equal to the temperature distribution during the liquid production operation. Therefore, there is no danger of damaging the piping of the room temperature line because the hot end side is not at a negative temperature and the low temperature fluid is not released at a low temperature when switching to the liquid production operation. .
(3) Since the liquefied heat exchanger does not repeat contraction and expansion, the durability life of the liquefied heat exchanger is improved.

また、本発明の請求項１に係る深冷空気液化分離装置によれば、液製造運転に際して、主熱交換器から出た原料空気の一部が複式精留塔に導入されるが、液製造運転に切換えられると、前記主熱交換器から出た原料空気の一部と共に、短時間のうちに高圧膨張タービンの膨張機で膨張されて寒冷を発生した原料空気が第５空気導入ラインを介して複式精留塔に導入される。従って、液製造運転への切換後、短時間のうちに効率よく液体窒素、液体酸素等を製造することができ、液製造運転のための稼動率が向上するから、低コストでより大量の液体窒素、液体酸素等を生産することができる。   Further, according to the chilled air liquefaction separation apparatus according to claim 1 of the present invention, part of the raw air discharged from the main heat exchanger is introduced into the double fractionator during the liquid production operation. When switched to operation, together with a part of the raw air that has come out of the main heat exchanger, the raw air that has been expanded in the expander of the high-pressure expansion turbine in a short period of time and has generated coldness passes through the fifth air introduction line. To be introduced into the double rectification column. Therefore, after switching to the liquid production operation, liquid nitrogen, liquid oxygen, etc. can be efficiently produced in a short time, and the operating rate for the liquid production operation is improved. Nitrogen, liquid oxygen, etc. can be produced.

以下、本発明の運転方法を実施する、実施の形態１乃至４に係る深冷空気液化分離装置を、その模式的系統図の図１乃至４を順次参照しながら説明する。先ず、本発明の実施の形態１に係る深冷空気液化分離装置を、その系統図の図１を参照しながら説明する。   Hereinafter, the cryogenic air liquefaction separation apparatus according to Embodiments 1 to 4 for carrying out the operation method of the present invention will be described with reference to FIGS. 1 to 4 of the schematic system diagrams. First, a cryogenic air liquefaction separation apparatus according to Embodiment 1 of the present invention will be described with reference to FIG.

図１に示す符号１は、本発明の形態１に係る深冷空気液化分離装置であって、この本発明の形態１に係る深冷空気液化分離装置１は、主として、原料空気圧縮機２と、予冷ユニット３ａと、吸着塔ユニット３ｂと、主熱交換器４と、昇圧圧縮機９ｂと、液化熱交換器７と、高圧膨張タービン１２と、複式精留塔１５と、これらに付随する付帯設備とから構成されている。   Reference numeral 1 shown in FIG. 1 is a chilled air liquefaction separation apparatus according to Embodiment 1 of the present invention. The chilled air liquefaction separation apparatus 1 according to Embodiment 1 of the present invention mainly includes a raw material air compressor 2 and The precooling unit 3a, the adsorption tower unit 3b, the main heat exchanger 4, the booster compressor 9b, the liquefaction heat exchanger 7, the high-pressure expansion turbine 12, the double rectification tower 15, and the incidentals associated therewith. It consists of equipment.

より詳しくは、深冷空気液化分離装置１は、原料空気圧縮機２で圧縮された原料空気を、主熱交換器４や液化熱交換器７に供給する空気供給元ライン３を備えている。この空気供給元ライン３には、原料空気圧縮機２側から下流側に向って順に、この原料空気圧縮機２で圧縮された原料空気を予冷するための予冷ユニット３ａが介装されると共に、この予冷ユニット３ａで１０〜４０℃に予冷された原料空気から水分・炭酸ガスを除去して精製する吸着塔ユニット３ｂが介装されている。この吸着塔ユニット３ｂは、交互に使用される第１吸着塔３ｂ１と、第２吸着塔３ｂ２とが並列に配設されてなる構成になっている。
なお、水分・炭酸ガスを除去するために、例えば第１吸着塔３ｂ１に原料空気が導入されている間に、第２吸着塔３ｂ２の吸着剤を再生するために、この第２吸着塔３ｂ２には、図示しないヒータで加熱したパージガスが供給され、水分・炭酸ガスを吸着した吸着剤が再生されるように構成されている。 More specifically, the chilled air liquefaction separation apparatus 1 includes an air supply source line 3 that supplies the raw air compressed by the raw air compressor 2 to the main heat exchanger 4 and the liquefied heat exchanger 7. The air supply source line 3 is provided with a precooling unit 3a for precooling the raw material air compressed by the raw material air compressor 2 in order from the raw material air compressor 2 to the downstream side, An adsorption tower unit 3b for removing water and carbon dioxide gas from the raw air precooled to 10 to 40 ° C. by the precooling unit 3a is interposed. The adsorption tower unit 3b has a configuration in which a first adsorption tower 3b 1 and a second adsorption tower 3b 2 that are used alternately are arranged in parallel.
In order to remove moisture / carbon dioxide gas, for example, this second adsorption tower is used to regenerate the adsorbent of the second adsorption tower 3b 2 while the raw air is being introduced into the first adsorption tower 3b 1. The purge gas heated by a heater (not shown) is supplied to 3b 2 so that the adsorbent adsorbing moisture / carbon dioxide gas is regenerated.

前記空気供給元ライン３の吸着塔ユニット３ｂより先端側は、主熱交換器４に連通しており、前記吸着塔ユニット３ｂにより精製された原料空気の一部が主熱交換器４に導入されるように構成されている。そして、前記主熱交換器４の出口から、上部塔１５ａと下部塔１５ｂとからなる複式精留塔１５の前記下部塔１５ｂに空気供給先ライン５が連通しており、前記空気供給元ライン３から導入されて液化点付近の温度になるまで冷却された原料空気が下部塔１５ｂに導入されるようになっている。   The front end side of the adsorption tower unit 3b of the air supply source line 3 communicates with the main heat exchanger 4, and part of the raw material air purified by the adsorption tower unit 3b is introduced into the main heat exchanger 4. It is comprised so that. An air supply destination line 5 communicates from the outlet of the main heat exchanger 4 to the lower column 15b of the double rectifying column 15 composed of an upper column 15a and a lower column 15b, and the air supply source line 3 The raw material air that has been introduced to the bottom and cooled to a temperature near the liquefaction point is introduced into the lower column 15b.

前記空気供給元ライン３の吸着塔ユニット３ｂと主熱交換器４との間から、液化熱交換器７に連通する第１空気導入ライン６が分岐している。この第１空気導入ライン６には、ガス製造運転中は開弁され、液製造運転中は閉弁される第１開閉弁Ｖ１が介装されており、前記吸着塔ユニット３ｂで精製された原料空気の残り（前記吸着塔ユニット３ｂから出た原料空気から前記主熱交換器４に導入された原料空気を差し引いた量）が液化熱交換器７に導入されるようになっている。そして、前記液化熱交換器７の出口から前記空気供給先ライン５の前記主熱交換器５と前記下部塔１５ｂとの間に、第２空気導入ライン８が連通している。この第２空気導入ライン８には、ガス製造運転中は開弁され、液製造運転中は閉弁される第２開閉弁Ｖ２が介装されており、前記第１空気導入ライン６から導入された原料空気が液化点近傍の温度になるまで冷却されて下部塔１５ｂに導入されるようになっている。 A first air introduction line 6 communicating with the liquefied heat exchanger 7 is branched from between the adsorption tower unit 3 b of the air supply source line 3 and the main heat exchanger 4. This first air inlet line 6, in the gas production runs is open, during fluid production runs are first on-off valve V 1 is interposed to be closed, said purified in the adsorption tower unit 3b The remainder of the raw material air (the amount obtained by subtracting the raw material air introduced into the main heat exchanger 4 from the raw material air output from the adsorption tower unit 3 b) is introduced into the liquefied heat exchanger 7. A second air introduction line 8 communicates from the outlet of the liquefied heat exchanger 7 between the main heat exchanger 5 of the air supply destination line 5 and the lower tower 15b. This second air introduction line 8, the gas production runs are opened, the liquid preparation operation is the second on-off valve V 2 is interposed which is closed, introduced from the first air introduction line 6 The raw material air thus cooled is cooled to a temperature near the liquefaction point and introduced into the lower column 15b.

前記第１空気導入ライン６の空気供給元ライン３との分岐部と、前記第１開閉弁Ｖ１との間から、液化熱交換器７に連通する空気導入元ライン９が分岐している。この空気導入元ライン９には、分岐側から液化熱交換器７に向って順に、入側開閉弁９ａと、この入側開閉弁９ａを通過した原料空気を３．０ＭＰａＧまで昇圧させる昇圧圧縮機９ｂが介装されている。そして、液化熱交換器７から前記下部塔１５ｂの前記空気供給先ライン５の連通位置の上側に、出側開閉弁１０ａが介装され、前記空気導入元ライン９から導入されると共に、液化熱交換器７により冷却されて液化した原料空気を導入する空気導入先ライン１０が連通している。 An air introduction source line 9 communicating with the liquefied heat exchanger 7 is branched from between a branch portion of the first air introduction line 6 with the air supply source line 3 and the first on-off valve V 1 . The air introduction source line 9 includes, in order from the branch side toward the liquefied heat exchanger 7, an inlet side on-off valve 9a and a booster compressor that boosts the raw material air that has passed through the inlet side on-off valve 9a to 3.0 MPaG. 9b is interposed. An outlet opening / closing valve 10a is interposed from the liquefied heat exchanger 7 to the upper side of the communication position of the air supply destination line 5 of the lower tower 15b, and is introduced from the air introduction source line 9, and the liquefaction heat An air introduction destination line 10 for introducing the raw material air cooled and liquefied by the exchanger 7 communicates.

前記空気導入元ライン９の昇圧圧縮機９ｂと、前記液化熱交換器７との間から第３空気導入ライン１１が分岐しており、この第３空気導入ライン１１は高圧膨張タービン１２の圧縮機１２ａを介して、前記第１空気導入ライン６の第１開閉弁Ｖ１と液化熱交換器７との間に連通している。この第３空気導入ライン１１の圧縮機１２ａ側と、第１空気導入ライン６の連通部との間に、ガス製造運転中は閉弁され、液製造運転中は開弁される第３開閉弁Ｖ３が介装されており、圧縮機１２ａで約５．０ＭＰａＧまで昇圧された後、液化熱交換器７に導入されるようになっている。 A third air introduction line 11 branches from between the boost compressor 9 b of the air introduction source line 9 and the liquefied heat exchanger 7, and the third air introduction line 11 is a compressor of the high pressure expansion turbine 12. through 12a, which communicates between the first on-off valve V 1 and liquefaction heat exchanger 7 of the first air introduction line 6. Between the compressor 12a side of the third air introduction line 11 and the communication portion of the first air introduction line 6, a third on-off valve is closed during the gas production operation and opened during the liquid production operation. V 3 is interposed, after being boosted to approximately 5.0MPaG by the compressor 12a, is adapted to be introduced into the liquefaction heat exchanger 7.

前記第１空気導入ライン６から導入された原料空気を前記第２空気導入ライン８に導く液化熱交換器７内の熱交換流路７ａの途中から、高圧膨張タービン１２の膨張機１２ｂに連通する第４空気導入ライン１３が分岐している。この第４空気導入ライン１３には、ガス製造運転中は閉弁され、液製造運転中は開弁される第４開閉弁Ｖ４が介装されている。
そして、前記高圧膨張タービン１２の膨張機１２ｂの出口は、第５空気導入ライン１４を介して前記空気供給先ライン５の前記第２空気導入ライン８の連通部と下部塔１５ｂとの間に連通している。そのため、液化熱交換器７で約−１００℃に冷却された原料空気が前記第４空気導入ライン１３から導入されると、前記膨張機１２ｂで約０．４５ＭＰａＧまで膨張されて寒冷を発生した原料空気が第５空気導入ライン１４を介して下部塔１５ｂに導入される。なお、前記第１開閉弁Ｖ１、第２開閉弁Ｖ２、第３開閉弁Ｖ３、第４開閉弁Ｖ４、入側開閉弁９ａ、および出側開閉弁１０ａは、ガス製造運転と、液製造運転の切換えに際して、遠隔操作により開閉操作される自動開閉弁である。 The raw material air introduced from the first air introduction line 6 communicates with the expander 12b of the high-pressure expansion turbine 12 from the middle of the heat exchange flow path 7a in the liquefied heat exchanger 7 that guides the raw air to the second air introduction line 8. The fourth air introduction line 13 is branched. This fourth air introduction line 13, the gas production runs are closed, the liquid preparation operation fourth on-off valve V 4 is interposed is opened.
The outlet of the expander 12b of the high-pressure expansion turbine 12 is communicated between the communication portion of the second air introduction line 8 of the air supply destination line 5 and the lower tower 15b via the fifth air introduction line 14. is doing. Therefore, when the raw material air cooled to about −100 ° C. by the liquefied heat exchanger 7 is introduced from the fourth air introduction line 13, the raw material is expanded to about 0.45 MPaG by the expander 12b and generates cold. Air is introduced into the lower tower 15 b through the fifth air introduction line 14. The first on-off valve V 1 , the second on-off valve V 2 , the third on-off valve V 3 , the fourth on-off valve V 4 , the inlet-side on-off valve 9a, and the outlet-side on-off valve 10a are used for gas production operation. It is an automatic on-off valve that is opened and closed by remote control when switching the liquid production operation.

前記複式精留塔１５の下部塔１５ｂの頂部に液体窒素供給ライン１６が設けられると共に、前記複式精留塔１５の上部塔１５ａの底部に液体酸素供給ライン１７が設けられている。また、前記複式精留塔１５の上部塔１５ａの頂部に窒素ガス供給ライン１８が、下部に酸素ガス供給ライン１９が設けられると共に、上下方向の中程より上方位置に廃ガス排出ライン１８ａが設けられている。なお、複式精留塔１５の上部塔１５ａの直下であって、かつ下部塔１５ｂ内の上部に設けられてなるものは、主凝縮器１５ｃである。   A liquid nitrogen supply line 16 is provided at the top of the lower column 15 b of the double rectifying column 15, and a liquid oxygen supply line 17 is provided at the bottom of the upper column 15 a of the double rectifying column 15. Further, a nitrogen gas supply line 18 is provided at the top of the upper column 15a of the double rectification column 15, an oxygen gas supply line 19 is provided at the lower portion, and a waste gas discharge line 18a is provided at a position higher than the middle in the vertical direction. It has been. The main condenser 15c is provided directly below the upper column 15a of the double rectification column 15 and at the upper part in the lower column 15b.

以下、本発明の実施の形態１に係る深冷空気液化分離装置１のガス製造運転と液製造運転について説明する。先ず、深冷空気液化分離装置１のガス製造運転について説明する。
即ち、原料空気圧縮機２で圧縮されて約９０℃に昇温した原料空気が予冷ユニット３ａで１０〜４０℃に予冷されると共に、予冷された原料空気が吸着塔ユニット３ｂに導入され、水分・炭酸ガスが除去されて精製される。そして、精製された原料空気の一部が主熱交換器４に導入され、液化点付近の温度になるまで冷却されて空気供給先ライン５を介して複式精留塔１５に供給される。また、これと並行して、吸着塔ユニット３ａで精製された原料空気の残りが第１空気導入ライン６（第１開閉弁Ｖ１開弁）から液化熱交換器７に導入され、液化点付近の温度になるまで冷却されて第２空気導入ライン８（第２開閉弁Ｖ２開弁）から空気供給先ライン５に合流し、前記主熱交換器４から出た原料空気の一部と共に複式精留塔１５の下部塔１５ｂに導入される。 Hereinafter, a gas production operation and a liquid production operation of the cryogenic air liquefaction separation apparatus 1 according to Embodiment 1 of the present invention will be described. First, the gas production operation of the cryogenic air liquefaction separation apparatus 1 will be described.
That is, the raw material air compressed by the raw material air compressor 2 and heated to about 90 ° C. is pre-cooled to 10 to 40 ° C. by the pre-cooling unit 3a, and the pre-cooled raw material air is introduced into the adsorption tower unit 3b. -Carbon dioxide gas is removed and purified. A part of the purified raw material air is introduced into the main heat exchanger 4, cooled to a temperature near the liquefaction point, and supplied to the double rectification column 15 through the air supply destination line 5. In parallel with this, it is introduced into liquefaction heat exchanger 7 remaining feed air which has been purified by adsorption column units 3a from the first air introduction line 6 (the first on-off valve V 1 open), near the liquefaction point is cooled to a temperature second air introduction line 8 merges from (the second on-off valve V 2 open) to the air supply destination line 5, double with a portion of the feed air exiting the main heat exchanger 4 It is introduced into the lower column 15 b of the rectifying column 15.

複式精留塔１５の下部塔１５ｂに導入された原料空気は、精留操作により上部塔１５ａの頂部に設けられた窒素ガス供給ライン１８に取出される窒素ガスと、上部塔１５ａの下部に設けられた酸素ガス供給ライン１９に取出される酸素ガスと、上部塔１５ａの上下方向の中程より上方位置に設けられた廃ガス排出ライン１８ａに取出される廃ガスと、必要に応じて生産されるアルゴンに分離される。窒素ガス供給ライン１８から取出された窒素ガスは、主熱交換器４で原料空気と熱交換を行って常温になって導出されると共に、図示しない窒素圧縮機で圧縮されて供給先に供給される。また、酸素ガス供給ライン１９から取出された酸素ガスは、主熱交換器４で原料空気と熱交換を行って常温になって導出されると共に、図示しない酸素圧縮機で圧縮されて供給先に供給される。そして、廃ガス排出ライン１８ａから取出された廃ガスは、液化熱交換器７で原料空気と熱交換を行って常温になって系外に放出される。   The raw air introduced into the lower column 15b of the double rectification column 15 is provided in the lower part of the upper column 15a and the nitrogen gas taken out to the nitrogen gas supply line 18 provided at the top of the upper column 15a by the rectification operation. The oxygen gas taken out to the oxygen gas supply line 19 and the waste gas taken out to the waste gas discharge line 18a provided at a position above the middle of the upper column 15a in the vertical direction are produced as necessary. Separated into argon. The nitrogen gas taken out from the nitrogen gas supply line 18 is led out at room temperature by exchanging heat with the raw material air in the main heat exchanger 4, and is compressed by a nitrogen compressor (not shown) and supplied to the supply destination. The Further, the oxygen gas taken out from the oxygen gas supply line 19 is led out at room temperature by exchanging heat with the raw air in the main heat exchanger 4, and is compressed by an oxygen compressor (not shown) to the supply destination. Supplied. And the waste gas taken out from the waste gas discharge line 18a is heat-exchanged with raw material air with the liquefied heat exchanger 7, becomes normal temperature, and is discharged | emitted out of the system.

次に、本発明の形態１に係る深冷空気液化分離装置１の液製造運転について説明する。
即ち、吸着塔ユニット３ｂで精製された原料空気は２分され、２分された原料空気の一部が主熱交換器４に導入されて、液化点付近の温度になるまで冷却される。主熱交換器４から出た原料空気の一部は、空気供給先ライン５から複式精留塔１５の下部塔１５ｂに導入される。原料空気の残りは、空気導入元ライン９（第１開閉弁Ｖ１閉弁、入側開閉弁９ａ開弁）を介して昇圧圧縮機９ｂに導入され、約３．０ＭＰａＧまで昇圧される。昇圧された原料空気の残りは２分され、２分された原料空気の残りの１部は、液化熱交換器７で液化され、液体製品を製造するための寒冷源として空気導入先ライン１０（出側開閉弁１０ａ開弁）から複式精留塔１５の下部塔１５ｂに導入される。 Next, the liquid manufacturing operation of the cryogenic air liquefaction separation apparatus 1 according to the first embodiment of the present invention will be described.
That is, the raw material air purified by the adsorption tower unit 3b is divided into two parts, and a part of the two-part raw material air is introduced into the main heat exchanger 4 and cooled to a temperature near the liquefaction point. Part of the raw material air that has exited from the main heat exchanger 4 is introduced from the air supply destination line 5 to the lower column 15 b of the double rectification column 15. The remaining feed air, the air introduction source line 9 (the first on-off valve V 1 closed, inlet-side on-off valve 9a open) is introduced into the booster compressor 9b through, it is boosted to about 3.0 MPaG. The remainder of the pressurized raw material air is divided into two parts, and the remaining part of the two-minute raw material air is liquefied by the liquefied heat exchanger 7 and is used as a cold source for producing a liquid product. From the outlet side on-off valve 10a) to the lower column 15b of the double rectification column 15.

また、２分された原料空気の残りの残りは第３空気導入ライン１１から高圧膨張タービン１２の圧縮機１２ａに導入されて約５．０ＭＰａＧになるまで圧縮された後、第３開閉弁Ｖ３、第１空気導入ライン６を経て液化熱交換器７に導入される。そして、この液化熱交換器７で約−１００℃に冷却された後に、第４空気導入ライン１３（第４開閉弁Ｖ４は開弁、第２開閉弁Ｖ２は閉弁）から高圧膨張タービン１２の膨張機１２ｂに導入される。
膨張機１２ｂに導入された、２分された原料空気の残りの残りは、約０．４５ＭＰａＧに膨張されて深冷空気液化分離装置１の液製造運転のための寒冷を発生した後、空気供給先ライン５に合流し、前記主熱交換器４から出た２分された原料空気の一部と共に複式精留塔１５の下部塔１５ｂに導入される。 Further, the remainder of the bifurcated raw material air is introduced from the third air introduction line 11 into the compressor 12a of the high-pressure expansion turbine 12 and compressed to about 5.0 MPaG, and then the third on-off valve V 3. Then, it is introduced into the liquefied heat exchanger 7 through the first air introduction line 6. After being cooled to about −100 ° C. by the liquefied heat exchanger 7, the high pressure expansion turbine is supplied from the fourth air introduction line 13 (the fourth on-off valve V 4 is opened and the second on-off valve V 2 is closed). 12 expanders 12b.
The remaining remainder of the bifurcated raw material air introduced into the expander 12b is expanded to about 0.45 MPaG to generate cold for the liquid manufacturing operation of the cryogenic air liquefaction separation apparatus 1, and then air supply It joins the first line 5 and is introduced into the lower column 15 b of the double rectification column 15 together with a part of the bisected raw material air that has come out of the main heat exchanger 4.

複式精留塔１５の下部塔１５ｂに導入された原料空気は、精留操作により上部塔１５ａの頂部に設けられた窒素ガス供給ライン１８から取出される窒素ガスと、上部塔１５ａの下部に設けられた酸素ガス供給ライン１９に取出される酸素ガスと、上部塔１５ａの上下方向の中程より上方位置に設けられた廃ガス排出ライン１８ａに取出される廃ガスと、下部塔１５ｂの頂部に設けられた液体窒素供給ライン１６に取出される液体窒素と、上部塔１５ａの底部に設けられた液体酸素供給ライン１７に取出される液体酸素と、必要に応じて生産されるアルゴンに分離される。   The raw air introduced into the lower column 15b of the double rectification column 15 is provided with nitrogen gas taken out from the nitrogen gas supply line 18 provided at the top of the upper column 15a by the rectification operation, and at the lower part of the upper column 15a. The oxygen gas taken out to the oxygen gas supply line 19 and the waste gas taken out to the waste gas discharge line 18a provided at a position higher than the middle in the vertical direction of the upper column 15a, and the top of the lower column 15b Liquid nitrogen taken out to the liquid nitrogen supply line 16 provided, liquid oxygen taken out to the liquid oxygen supply line 17 provided at the bottom of the upper column 15a, and argon produced as necessary are separated. .

前記窒素ガス供給ライン１８から取出された窒素ガスは、主熱交換器４で原料空気と熱交換を行って常温になって導出され、図示しない窒素圧縮機で圧縮されて供給先に供給される。前記酸素ガス供給ライン１９から取出された酸素ガスは、主熱交換器４で原料空気と熱交換を行って常温になって導出され、図示しない酸素圧縮機で圧縮されて供給先に供給される。前記廃ガス排出ライン１８ａから取出された廃ガスは、液化熱交換器７で原料空気と熱交換を行って常温になって導出される。そして、前記液体窒素供給ライン１６から取出された液体窒素は、図示しない液体窒素タンクに送られ、液体酸素供給ライン１７から取出される液体酸素は、図示しない液体酸素タンクに送られる。なお、この実施の形態１の場合には、液体窒素と液体酸素の両方を製造するようにしているが、液体窒素と液体酸素のうち何れか一方を製造するようにしても良い。   The nitrogen gas taken out from the nitrogen gas supply line 18 is led out at room temperature by exchanging heat with the raw air in the main heat exchanger 4, compressed by a nitrogen compressor (not shown), and supplied to the supply destination. . The oxygen gas taken out from the oxygen gas supply line 19 is led out at room temperature by exchanging heat with the raw air in the main heat exchanger 4, compressed by an oxygen compressor (not shown), and supplied to the supply destination. . The waste gas taken out from the waste gas discharge line 18a is exchanged with the raw material air in the liquefied heat exchanger 7 to be brought out to room temperature. Then, the liquid nitrogen taken out from the liquid nitrogen supply line 16 is sent to a liquid nitrogen tank (not shown), and the liquid oxygen taken out from the liquid oxygen supply line 17 is sent to a liquid oxygen tank (not shown). In the first embodiment, both liquid nitrogen and liquid oxygen are produced. However, either one of liquid nitrogen and liquid oxygen may be produced.

本発明の実施の形態１に係る深冷空気液化分離装置１では、上記のとおり、ガス製造運転と液製造運転とが交互に繰り返されるのであるが、液化熱交換器７は液製造運転中のみならず、ガス製造運転中も熱交換器として作動されるように構成されている。従って、本発明の実施の形態１に係る深冷空気液化分離装置１によれば、下記のとおりの効果を得ることができる。   In the chilled air liquefaction separation apparatus 1 according to Embodiment 1 of the present invention, as described above, the gas production operation and the liquid production operation are alternately repeated, but the liquefaction heat exchanger 7 is only in the liquid production operation. Instead, it is configured to operate as a heat exchanger even during gas production operation. Therefore, according to the cryogenic air liquefaction separation apparatus 1 according to Embodiment 1 of the present invention, the following effects can be obtained.

（１）ガス製造運転中の液化熱交換器７のガス出入り口間の温度分布は、液製造運転中における温度分布とほぼ同等に保持されていて、ガス製造運転から液製造運転に切換えるに際して冷却運転をする必要がないため、極めて短時間のうちにガス製造運転中の深冷空気液化分離装置１を液製造運転に移行させることができる。これにより、実質的な液製造運転時間が増加し、液体酸素・窒素等の生産性が向上するため、それら液体酸素・窒素等のコスト低減に大いに寄与することができる。
（２）ガス製造運転中の液化熱交換器のガス出入り口間の温度分布は、液製造運転中における温度分布とほぼ同等に保持されている。従って、温端側がマイナスの温度になっているということがなく、液製造運転への切換え時に低温流体が低温のまま放出されることがないため、常温ラインの配管が損傷するという危険性がない。
（３）液化熱交換器７は収縮と膨張とを繰り返すことがないため、液化熱交換器の耐久寿命が向上する。 (1) The temperature distribution between the gas inlet and outlet of the liquefied heat exchanger 7 during the gas production operation is maintained substantially equal to the temperature distribution during the liquid production operation, and the cooling operation is performed when switching from the gas production operation to the liquid production operation. Therefore, the chilled air liquefaction separation apparatus 1 during the gas production operation can be shifted to the liquid production operation in a very short time. Thereby, substantial liquid manufacturing operation time increases and productivity of liquid oxygen, nitrogen, etc. improves, Therefore It can contribute greatly to the cost reduction of these liquid oxygen, nitrogen, etc.
(2) The temperature distribution between the gas inlets and outlets of the liquefied heat exchanger during the gas production operation is maintained substantially equal to the temperature distribution during the liquid production operation. Therefore, there is no danger of damaging the piping of the room temperature line because the hot end side is not at a negative temperature and the low temperature fluid is not released at a low temperature when switching to the liquid production operation. .
(3) Since the liquefied heat exchanger 7 does not repeatedly contract and expand, the durability life of the liquefied heat exchanger is improved.

本発明の運転方法を実施する、本発明の実施の形態２に係る深冷空気液化分離装置を、その系統図の図２を参照しながら説明する。本発明の実施の形態２が上記実施の形態１と相違するところは、図１と図２との比較において、良く理解されるように、空気供給元ライン３の第１空気導入ライン６の分岐部と、第１空気導入ライン６の空気導入元ライン９の分岐部との間から、吸着塔ユニット３ｂで精製された原料空気の一部を分流させる第１空気分流ラインを設けたところにあるから、上記実施の形態と同一のものには同一符号を付し、その相違する点について説明する。   A cryogenic air liquefaction separation apparatus according to a second embodiment of the present invention that implements the operation method of the present invention will be described with reference to FIG. 2 of the system diagram thereof. The difference of the second embodiment of the present invention from the first embodiment is that the first air introduction line 6 of the air supply source line 3 is branched as will be well understood in the comparison between FIG. 1 and FIG. And a first air diversion line for diverting a part of the raw material air purified by the adsorption tower unit 3b from between the first air introduction line 6 and the branch part of the air introduction source line 9 of the first air introduction line 6. Therefore, the same components as those in the above embodiment are denoted by the same reference numerals, and different points will be described.

即ち、本発明の実施の形態２に係る深冷空気液化分離装置１ａでは、空気供給元ライン３の第１空気導入ライン６の分岐部と、第１空気導入ライン６の空気導入元ライン９の分岐部との間から、吸着塔ユニット３ｂで精製された原料空気を分流させる第１空気分流ライン２０が分岐している。そして、この第１空気分流ライン２０の先端側は、液化熱交換器７を介して、前記主熱交換器４から前記複式精留塔１５の下部塔１５ｂに連通する空気供給先ライン５に合流しており、ガス製造運転中、液製造運転中の如何を問わず、常時吸着塔ユニット３ｂで精製された原料空気の一部が液化点付近の温度になるまで冷却されて複式精留塔１５の下部塔１５ｂに導入されるように構成されている。   That is, in the chilled air liquefaction separation device 1a according to Embodiment 2 of the present invention, the branch portion of the first air introduction line 6 of the air supply source line 3 and the air introduction source line 9 of the first air introduction line 6 are connected. A first air branch line 20 for branching the raw air purified by the adsorption tower unit 3b branches from between the branch portions. And the front end side of this 1st air distribution line 20 joins the air supply destination line 5 connected to the lower column 15b of the said double rectification column 15 from the said main heat exchanger 4 via the liquefying heat exchanger 7. During the gas production operation and the liquid production operation, the double rectification tower 15 is cooled by cooling until part of the raw material air purified by the adsorption tower unit 3b reaches a temperature near the liquefaction point. It is comprised so that it may introduce into the lower tower 15b.

本発明の実施の形態２に係る深冷空気液化分離装置１ａでは、上記実施の形態１に係る深冷空気液化分離装置１の場合と同様に、ガス製造運転中、液製造運転中の如何を問わず、液化熱交換器７が作動している。これに加えて、液化熱交換器７に対して、常時吸着塔ユニット３ｂで精製された原料空気の一部が導入されて熱交換する。従って、上記実施の形態２に係る深冷空気液化分離装置１ａによれば、上記実施の形態１に係る深冷空気液化分離装置１と同様の効果が得られるのに加えて、主熱交換器４と液化熱交換器７との熱バランス状態をより良好にすることができるという優れた効果が得られる。   In the chilled air liquefaction separation apparatus 1a according to the second embodiment of the present invention, as in the case of the chilled air liquefaction separation apparatus 1 according to the first embodiment, whether the gas production operation or the liquid production operation is in progress. Regardless, the liquefied heat exchanger 7 is operating. In addition to this, a part of the raw material air purified by the adsorption tower unit 3b is always introduced into the liquefied heat exchanger 7 for heat exchange. Therefore, according to the chilled air liquefaction separation apparatus 1a according to the second embodiment, in addition to obtaining the same effect as the chilled air liquefaction separation apparatus 1 according to the first embodiment, the main heat exchanger The outstanding effect that the heat balance state of 4 and the liquefied heat exchanger 7 can be made more favorable is acquired.

本発明の運転方法を実施する、本発明の実施の形態３に係る深冷空気液化分離装置を、その系統図の図３を参照しながら説明する。本発明の実施の形態３が上記実施の形態１と相違するところは、図１と図３との比較において、良く理解されるように、空気供給元ライン３の第１空気導入ライン６の分岐部と、第１空気導入ライン６の空気導入元ライン９の分岐部との間から、吸着塔ユニット３ｂで精製された原料空気の一部を分流させる第２空気分流ラインを設け、これに寒冷発生手段を設けたところにあるから、上記実施の形態と同一のものには同一符号を付し、その相違する点について説明する。   A cryogenic air liquefaction separation apparatus according to a third embodiment of the present invention that implements the operation method of the present invention will be described with reference to FIG. 3 of the system diagram thereof. The third embodiment of the present invention differs from the first embodiment in that the first air introduction line 6 of the air supply source line 3 is branched as will be well understood in the comparison between FIG. 1 and FIG. And a second air diversion line for diverting part of the raw material air purified by the adsorption tower unit 3b from between the first air introduction line 6 and the branch portion of the air introduction source line 9 of the first air introduction line 6 are provided. Since the generating means is provided, the same components as those in the above embodiment are denoted by the same reference numerals, and different points will be described.

即ち、本発明の実施の形態３に係る深冷空気液化分離装置１ｂでは、空気供給元ライン３の第１空気導入ライン６の分岐部と、第１空気導入ライン６の空気導入元ライン９の分岐部との間から、吸着塔ユニット３ｂで精製された原料空気を分流させる第２空気分流ライン２１が分岐している。そして、この空気分流ライン２１の先端側は、低圧膨張タービン２２の圧縮機２２ａ、主熱交換器４、低圧膨張タービン２２の膨張機２２ｂを経て前記複式精留塔１５の上部塔１５ａに連通しており、ガス製造運転中、液製造運転中の如何を問わず、膨張タービン２２の膨張機２２ｂで装置の運転維持に必要な寒冷を発生し、常時複式精留塔１５の上部塔１５ａに導入されるように構成されている。   That is, in the chilled air liquefaction separation apparatus 1b according to Embodiment 3 of the present invention, the branch portion of the first air introduction line 6 of the air supply source line 3 and the air introduction source line 9 of the first air introduction line 6 are connected. A second air diversion line 21 for diverting the raw material air purified by the adsorption tower unit 3b is branched from between the branch portions. The leading end side of the air branch line 21 communicates with the upper column 15a of the double rectifying column 15 via the compressor 22a of the low pressure expansion turbine 22, the main heat exchanger 4, and the expander 22b of the low pressure expansion turbine 22. During the gas production operation and the liquid production operation, the expander 22b of the expansion turbine 22 generates the cold necessary to maintain the operation of the apparatus, and is always introduced into the upper column 15a of the double rectification column 15. It is configured to be.

そのため、本発明の実施の形態３に係る深冷空気液化分離装置１ｂによれば、上記実施の形態１に係る深冷空気液化分離装置１の場合と同様に、ガス製造運転中、液製造運転中の如何を問わず、液化熱交換器７が作動している。これに加えて、吸着塔ユニット３ｂで精製された原料空気の一部が低圧膨張タービン２２の圧縮機２２ａで約０．９ＭＰａＧまで昇圧されて主熱交換器４で約−１００℃まで冷却された後、低圧膨張タービン２２の膨張機２２ｂで約０．０３ＭＰａＧに膨張されて深冷空気液化分離装置１ｂの運転維持に必要な寒冷を発生し、常時複式精留塔１５の上部塔１５ａに導入される。   Therefore, according to the chilled air liquefaction separation apparatus 1b according to Embodiment 3 of the present invention, as in the case of the chilled air liquefaction separation apparatus 1 according to Embodiment 1, the liquid manufacturing operation is performed during the gas manufacturing operation. Regardless of the inside, the liquefied heat exchanger 7 is operating. In addition, a part of the raw material air purified by the adsorption tower unit 3b was pressurized to about 0.9 MPaG by the compressor 22a of the low-pressure expansion turbine 22 and cooled to about −100 ° C. by the main heat exchanger 4. Thereafter, it is expanded to about 0.03 MPaG by the expander 22b of the low-pressure expansion turbine 22 to generate cold necessary for maintaining the operation of the cryogenic air liquefaction separation apparatus 1b, and is always introduced into the upper column 15a of the double rectification column 15. The

従って、本発明の実施の形態３に係る深冷空気液化分離装置１ｂによれば、上記実施の形態１に係る深冷空気液化分離装置１と同様の効果が得られるのに加えて、高圧膨張タービン１２の運転停止中、つまりガス製造運転中においても、低圧膨張タービン２２の膨張機２２ｂから寒冷を発生した原料空気が複式精留塔に常時供給されるため、深冷空気液化分離装置１ｂの運転維持に必要な寒冷を外部から補給する必要がない。   Therefore, according to the cryogenic air liquefaction separation apparatus 1b according to Embodiment 3 of the present invention, in addition to obtaining the same effect as the cryogenic air liquefaction separation apparatus 1 according to Embodiment 1, the high pressure expansion Even when the operation of the turbine 12 is stopped, that is, during the gas production operation, the raw air that has generated cold is constantly supplied from the expander 22b of the low-pressure expansion turbine 22 to the double rectification tower. There is no need to replenish the coldness necessary to maintain operation.

本発明の運転方法を実施する、本発明の実施の形態４に係る深冷空気液化分離装置を、その系統図の図４を参照しながら説明する。本発明の実施の形態４が上記実施の形態１と相違するところは、図１と図２乃至４との比較において良く理解されるように、本発明の実施の形態１に係る深冷空気液化分離装置１に、本発明の実施の形態２に係る深冷空気液化分離装置１ａに設けた第１空気分流ラインと、本発明の実施の形態３に係る深冷空気液化分離装置１ｂに設けた寒冷発生手段を備えた第２空気分流ライン２１とを設けたものであるから、上記実施の形態と同一のものには同一符号を付し、その相違する点について説明する。   A cryogenic air liquefaction separation apparatus according to a fourth embodiment of the present invention that implements the operation method of the present invention will be described with reference to FIG. 4 of the system diagram thereof. The difference of the fourth embodiment of the present invention from the first embodiment is that the chilled air liquefaction according to the first embodiment of the present invention is well understood in the comparison between FIG. 1 and FIGS. The separation device 1 is provided in the first air branch line provided in the chilled air liquefaction separation device 1a according to Embodiment 2 of the present invention, and in the chilled air liquefaction separation device 1b according to Embodiment 3 of the present invention. Since the second air distribution line 21 provided with the cold generation means is provided, the same components as those in the above embodiment are denoted by the same reference numerals, and different points will be described.

即ち、本発明の実施の形態４に係る深冷空気液化分離装置１ｃでは、空気供給元ライン３の第１空気導入ライン６の分岐部と、第１空気導入ライン６の空気導入元ライン９の分岐部との間から、吸着塔ユニット３ｂで精製された原料空気を分流させる第１空気分流ライン２０が分岐している。そして、この第１空気分流ライン２０の先端側は、液化熱交換器７を介して、前記主熱交換器４から前記複式精留塔１５の下部塔１５ｂに連通する空気供給先ライン５に合流しており、ガス製造運転中、液製造運転中の如何を問わず、常時吸着塔ユニット３ｂで精製された原料空気の一部が液化点付近の温度になるまで冷却されて複式精留塔１５の下部塔１５ｂに導入されるように構成されている。   That is, in the chilled air liquefaction separation apparatus 1c according to Embodiment 4 of the present invention, the branch portion of the first air introduction line 6 of the air supply source line 3 and the air introduction source line 9 of the first air introduction line 6 are connected. A first air branch line 20 for branching the raw air purified by the adsorption tower unit 3b branches from between the branch portions. And the front end side of this 1st air distribution line 20 joins the air supply destination line 5 connected to the lower column 15b of the said double rectification column 15 from the said main heat exchanger 4 via the liquefying heat exchanger 7. During the gas production operation and the liquid production operation, the double rectification tower 15 is cooled by cooling until part of the raw material air purified by the adsorption tower unit 3b reaches a temperature near the liquefaction point. It is comprised so that it may introduce into the lower tower 15b.

また、空気供給元ライン３の第１空気導入ライン６の分岐部と、第１空気導入ライン６の空気導入元ライン９の分岐部との間から、吸着塔ユニット３ｂによって精製された原料空気を分流させる第２空気分流ライン２１が分岐している。そして、この空気分流ライン２１の先端側は、低圧膨張タービン２２の圧縮機２２ａ、主熱交換器４、低圧膨張タービン２２の膨張機２２ｂを経て前記複式精留塔１５の上部塔１５ａに連通しており、ガス製造運転中、液製造運転中の如何を問わず、膨張タービン２２の膨張機２２ｂで装置の運転維持に必要な寒冷を発生し、常時複式精留塔１５の上部塔１５ａに導入されるように構成されている。   In addition, the raw material air purified by the adsorption tower unit 3b is taken between the branch portion of the first air introduction line 6 of the air supply source line 3 and the branch portion of the air introduction source line 9 of the first air introduction line 6. A second air branch line 21 for branching is branched. The leading end side of the air branch line 21 communicates with the upper column 15a of the double rectifying column 15 via the compressor 22a of the low pressure expansion turbine 22, the main heat exchanger 4, and the expander 22b of the low pressure expansion turbine 22. During the gas production operation and the liquid production operation, the expander 22b of the expansion turbine 22 generates the cold necessary to maintain the operation of the apparatus, and is always introduced into the upper column 15a of the double rectification column 15. It is configured to be.

本発明の実施の形態４に係る深冷空気液化分離装置１ｃでは、上記実施の形態１に係る深冷空気液化分離装置１の場合と同様に、ガス製造運転中、液製造運転中の如何を問わず、液化熱交換器７が作動している。これに加えて、液化熱交換器７に、常時吸着塔ユニット３ｂで精製された原料空気の一部が導入されると共に、低圧膨張タービン２２の膨張機２２ｂによって装置の運転維持に必要な寒冷を発生している。   In the chilled air liquefaction separation apparatus 1c according to the fourth embodiment of the present invention, as in the case of the chilled air liquefaction separation apparatus 1 according to the first embodiment, whether the gas production operation or the liquid production operation is in progress. Regardless, the liquefied heat exchanger 7 is operating. In addition to this, a part of the raw material air always purified by the adsorption tower unit 3b is introduced into the liquefied heat exchanger 7, and the cooling required for maintaining the operation of the apparatus is performed by the expander 22b of the low-pressure expansion turbine 22. It has occurred.

従って、本発明の実施の形態４に係る深冷空気液化分離装置１ｃによれば、上記実施の形態１に係る深冷空気液化分離装置１と同様の効果が得られ、さらに上記実施の形態１ａ，１ｂの効果、即ち主熱交換器４と液化熱交換器７との熱バランス状態をより良好にすることができるという優れた効果が得られる。また、ガス製造運転中においても、低圧膨張タービン２２の膨張機２２ｂから寒冷を発生した原料空気が複式精留塔に常時供給されるため、深冷空気液化分離装置１ｂの運転維持に必要な寒冷を外部から補給する必要がないという効果が得られる。   Therefore, according to the chilled air liquefaction separation apparatus 1c according to the fourth embodiment of the present invention, the same effects as those of the chilled air liquefaction separation apparatus 1 according to the first embodiment can be obtained, and further the first embodiment 1a. , 1b, that is, the excellent heat balance state between the main heat exchanger 4 and the liquefied heat exchanger 7 can be obtained. Further, even during the gas production operation, the raw material air that has generated cold is constantly supplied from the expander 22b of the low-pressure expansion turbine 22 to the double rectification tower. Therefore, the cold air necessary for maintaining the operation of the deep air liquefaction separation apparatus 1b is maintained. The effect that it is not necessary to replenish from the outside is obtained.

以上説明した本発明の運転方法を実施する、本発明の上記実施の形態１乃至４に係る深冷空気液化分離装置１乃至１ｃは本発明の具体例に過ぎず、本発明の技術的思想を逸脱しない範囲内における設計変更等は自由自在である。従って、深冷空気液化分離装置の形態は、上記実施の形態１乃至４に係る深冷空気液化分離装置１乃至１ｃの構成に限定されるものではない。   The chilled air liquefaction separation apparatuses 1 to 1c according to the first to fourth embodiments of the present invention that implement the operation method of the present invention described above are only specific examples of the present invention, and the technical idea of the present invention is achieved. Design changes and the like within a range that does not deviate are free. Therefore, the form of the chilled air liquefaction separation apparatus is not limited to the configuration of the chilled air liquefaction separation apparatuses 1 to 1c according to the first to fourth embodiments.

本発明の実施の形態１に係る深冷空気液化分離装置の系統図である。It is a systematic diagram of the cryogenic air liquefaction separation apparatus which concerns on Embodiment 1 of this invention. 本発明の実施の形態２に係る深冷空気液化分離装置の系統図である。It is a systematic diagram of the cryogenic air liquefaction separation apparatus which concerns on Embodiment 2 of this invention. 本発明の実施の形態３に係る深冷空気液化分離装置の系統図である。It is a systematic diagram of the cryogenic air liquefaction separation apparatus which concerns on Embodiment 3 of this invention. 本発明の実施の形態４に係る深冷空気液化分離装置の系統図である。It is a systematic diagram of the cryogenic air liquefaction separation apparatus which concerns on Embodiment 4 of this invention. 従来例に係り、一般的な液化装置付きの深冷空気液化分離装置の系統図である。It is a systematic diagram of the cryogenic air liquefaction separation apparatus with a general liquefaction apparatus concerning a prior art example.

符号の説明Explanation of symbols

１，１ａ，１ｂ，１ｃ…深冷空気液化分離装置
２…原料空気圧縮機
３…空気供給元ライン，３ａ…予冷ユニット，３ｂ…吸着塔ユニット，３ｂ１…第１吸着塔，３ｂ２…第２吸着塔
４…主熱交換器
５…空気供給先ライン
６…第１空気導入ライン
７…液化熱交換器，７ａ…熱交換流
８…第２空気導入ライン
９…空気導入元ライン，９ａ…入側開閉弁，９ｂ…昇圧圧縮機
１０…空気導入先ライン，１０ａ…出側開閉弁
１１…第３空気導入ライン
１２…高圧膨張タービン，１２ａ…圧縮機，１２ｂ…膨張機
１３…第４空気導入ライン
１４…第５空気導入ライン
１５…複式精留塔，１５ａ…上部塔，１５ｂ…下部塔，１５ｃ…アルゴン精製装置
１６…液体窒素供給ライン
１７…液体酸素供給ライン
１８…窒素ガス供給ライン，１８ａ…廃ガス排出ライ
１９…酸素ガス供給ライン
２０…第１空気分流ライン
２１…第２空気分流ライン
２２…低圧膨張タービン，２２ａ…圧縮機，２２ｂ…膨張機 DESCRIPTION OF SYMBOLS 1, 1a, 1b, 1c ... Cryogenic air liquefaction separation apparatus 2 ... Raw material air compressor 3 ... Air supply source line, 3a ... Pre-cooling unit, 3b ... Adsorption tower unit, 3b 1 ... 1st adsorption tower, 3b 2 ... 1st 2 adsorption tower 4 ... main heat exchanger 5 ... air supply destination line 6 ... first air introduction line 7 ... liquefied heat exchanger, 7a ... heat exchange flow 8 ... second air introduction line 9 ... air introduction source line, 9a ... Inlet side open / close valve, 9b ... Boost compressor 10 ... Air introduction destination line, 10a ... Out side on / off valve 11 ... Third air introduction line 12 ... High pressure expansion turbine, 12a ... Compressor, 12b ... Expander 13 ... Fourth air Introduction line 14 ... Fifth air introduction line 15 ... Multiple rectification column, 15a ... Upper column, 15b ... Lower column, 15c ... Argon purification device 16 ... Liquid nitrogen supply line 17 ... Liquid oxygen supply line 18 ... Nitrogen gas supply line, 18a ... Gas discharge line 19 ... oxygen gas supply line 20 ... first air diversion line 21 ... second air diversion line 22 ... a low-pressure expansion turbine, 22a ... compressor, 22b ... expander

Claims (2)

原料空気圧縮機と、この原料空気圧縮機で圧縮された原料空気を予冷する予冷ユニットと、この予冷ユニットで予冷された原料空気から水分・炭酸ガスを除去して精製する吸着塔ユニットと、この吸着塔ユニットで精製された原料空気の一部を冷却する主熱交換器と、前記吸着塔ユニットで精製された原料空気の残りを圧縮する昇圧圧縮機と、この昇圧圧縮機で昇圧された原料空気の一部を液化するための液化熱交換器と、前記昇圧圧縮機で圧縮された原料空気の残りの一部を膨張させて寒冷を発生させる高圧膨張タービンと、前記主熱交換器、液化熱交換器を経て導入された原料空気を窒素と酸素等に精留分離する複式精留塔と、これらに付随する付帯設備とを備えると共に、ガス製造運転と液製造運転とに切換え操作される深冷空気液化分離装置において、前記ガス製造運転中は開弁され、前記液製造運転中は閉弁される第１開閉弁が介装され、前記吸着塔ユニットで精製された原料空気の残りを前記液化熱交換器に導入する第１空気導入ラインと、前記ガス製造運転中は開弁され、前記液製造運転中は閉弁される第２開閉弁が介装され、前記液化熱交換器から出た原料空気を複式精留塔に導入する第２空気導入ラインと、前記ガス製造運転中は閉弁され、前記液製造運転中は開弁される第３開閉弁が介装され、前記高圧膨張タービンの圧縮機側から出た原料空気を前記液化熱交換器に導入する第３空気導入ラインと、前記ガス製造運転中は閉弁され、前記液製造運転中は開弁される第４開閉弁が介装され、前記液化熱交換器から出た原料空気を前記高圧膨張タービンの膨張機側に導入する第４空気導入ラインと、液製造運転に際して前記第４空気導入ラインから導入され、前記高圧膨張タービンの膨張機で膨張されて寒冷を発生した原料空気を複式精留塔に導入する第５空気導入ラインを備えたことを特徴とする深冷空気液化分離装置。   A raw air compressor, a pre-cooling unit for pre-cooling the raw air compressed by the raw air compressor, an adsorption tower unit for removing water and carbon dioxide gas from the raw air pre-cooled by the pre-cooling unit, and a purification unit A main heat exchanger that cools part of the raw material air purified by the adsorption tower unit, a booster compressor that compresses the remainder of the raw material air purified by the adsorption tower unit, and a raw material that has been pressurized by the booster compressor A liquefied heat exchanger for liquefying a part of the air; a high-pressure expansion turbine for expanding the remaining part of the raw material air compressed by the booster compressor to generate cold; the main heat exchanger; It is equipped with a double rectification column for rectifying and separating raw material air introduced through a heat exchanger into nitrogen and oxygen, etc., and ancillary equipment associated therewith, and is switched between a gas production operation and a liquid production operation. Chilled air liquefaction In the separation apparatus, a first on-off valve that is opened during the gas production operation and closed during the liquid production operation is interposed, and the remaining raw material air purified by the adsorption tower unit is exchanged with the liquefaction heat. The first air introduction line to be introduced into the vessel and a second on-off valve that is opened during the gas production operation and closed during the liquid production operation are provided, and the raw material air discharged from the liquefied heat exchanger And a third open / close valve that is closed during the gas production operation and is opened during the liquid production operation, and compresses the high-pressure expansion turbine. A third air introduction line for introducing the raw air discharged from the machine side into the liquefied heat exchanger, and a fourth on-off valve that is closed during the gas production operation and opened during the liquid production operation. The raw material air from the liquefied heat exchanger is expanded into the expander of the high pressure expansion turbine. A fourth air introduction line to be introduced into the rectifying column, and a raw air introduced from the fourth air introduction line during the liquid production operation and expanded by the expander of the high-pressure expansion turbine to generate cold. 5. A cryogenic air liquefaction separation apparatus comprising an air introduction line. 原料空気を原料空気圧縮機で圧縮し、原料空気圧縮機から出た原料空気を予冷ユニットで予冷し、予冷した原料空気を水分・炭酸ガスを除去する吸着塔ユニットに導入し、この吸着塔ユニットから出た原料空気の一部を主熱交換器に導入し、残りの原料空気を液化熱交換器に導入すると共に、前記主熱交換器、および液化熱交換器から出た原料空気を複式精留塔に導入して窒素ガスと酸素ガス等を製造するガス製造運転と、前記吸着塔ユニットから出た原料空気の一部を主熱交換器に導入し、残りの原料空気を昇圧圧縮機で昇圧させた後に二分し、二分した一方の原料空気を液化熱交換器に導入し、二分した他方の原料空気を高圧膨張タービンの圧縮機で圧縮して液化熱交換器に導入し、この液化熱交換器から出た原料空気を高圧膨張タービンの膨張機で膨張させた後に複式精留塔に導入すると共に、前記主熱交換器から出た原料空気の一部、および前記液化熱交換器から出た二分した一方の原料空気を複式精留塔に導入して液体窒素と液体酸素等を製造する液製造運転とを、自動切換することを特徴とする深冷空気液化分離装置の運転方法。   This adsorbing tower unit compresses the raw material air with the raw material air compressor, precools the raw material air from the raw material air compressor with the precooling unit, and introduces the precooled raw material air into the adsorption tower unit that removes moisture and carbon dioxide gas. A part of the raw material air discharged from the main heat exchanger is introduced into the main heat exchanger, the remaining raw material air is introduced into the liquefied heat exchanger, and the raw air discharged from the main heat exchanger and the liquefied heat exchanger is combined with the double precision. A gas production operation for producing nitrogen gas, oxygen gas, etc. by introducing into the distillation column, and introducing a part of the raw material air from the adsorption tower unit into the main heat exchanger, and the remaining raw material air with a booster compressor After the pressure is increased, the gas is divided into two parts, one of the two raw material air is introduced into the liquefied heat exchanger, and the other half of the raw material air is compressed by the compressor of the high-pressure expansion turbine and introduced into the liquefied heat exchanger. The raw air from the exchanger is After being expanded by an expander of the above, and introduced into a double rectification column, and a part of the raw material air exiting from the main heat exchanger and one half of the raw air exiting from the liquefied heat exchanger are subjected to double rectification A method for operating a cryogenic air liquefaction separation apparatus, wherein a liquid production operation for producing liquid nitrogen, liquid oxygen, and the like introduced into a tower is automatically switched.
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