TWI525298B - Air liquefaction separation method and device - Google Patents
Air liquefaction separation method and device Download PDFInfo
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- TWI525298B TWI525298B TW099124121A TW99124121A TWI525298B TW I525298 B TWI525298 B TW I525298B TW 099124121 A TW099124121 A TW 099124121A TW 99124121 A TW99124121 A TW 99124121A TW I525298 B TWI525298 B TW I525298B
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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
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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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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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
- F25J3/04248—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
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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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04339—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air
- F25J3/04345—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air and comprising a gas work expansion loop
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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
- F25J3/04248—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
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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
- F25J3/04406—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
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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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
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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
- 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
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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
本發明係關於一種空氣液化分離方法及裝置，詳細而言，係關於一種藉由利用中壓塔及低壓塔，將經壓縮、純化、冷卻之原料空氣加以深冷分離，而至少提取液態氧作為產品之空氣液化分離方法及裝置。The present invention relates to an air liquefaction separation method and apparatus, and more particularly to a method for utilizing a medium pressure column and a low pressure column to cryogenically separate compressed, purified, and cooled raw material air, and at least extracting liquid oxygen as Air liquefaction separation method and device for products.
工業上製造氧、氮及氬時，通常係藉由以空氣為原料，利用由中壓塔、低壓塔所構成之複式精餾塔(compound rectifying column)進行分離之所謂深冷式空氣液化分離裝置進行製造。於該深冷式空氣液化分離裝置中，可將產品之5%左右製造成液態氧、液態氮、液體氬。但是，當製作更多之液體產品時，則必須追加液化程序。When manufacturing oxygen, nitrogen and argon in the industry, it is usually a so-called deep-cooling air liquefaction separation device which uses air as a raw material and separates it by a compound rectifying column composed of a medium pressure column and a low pressure column. Made for manufacturing. In the cryogenic air liquefaction separation apparatus, about 5% of the product can be produced into liquid oxygen, liquid nitrogen, and liquid argon. However, when making more liquid products, a liquefaction procedure must be added.
液化程序係使原料空氣、氮氣等壓縮、循環、絕熱膨脹而獲得程序中所需之寒冷者，關於各個程序，已揭示有多種技術(例如，參照專利文獻1)。The liquefaction procedure is such that the raw material air, nitrogen gas, or the like is compressed, circulated, and adiabatically expanded to obtain a cold required for the procedure. Various techniques have been disclosed for each program (for example, refer to Patent Document 1).
於上述液化程序中，係將循環流體經部分液化之狀態供給至蒸餾塔，提取熱平衡之液體產品。與將低壓及/或中壓之氮氣加以壓縮而形成循環流體之氮循環液化程序相比，將高壓之原料空氣之一部分加以壓縮，而形成循環流體的空氣循環液化程序中，壓縮循環流體所需之動力消耗較少，故為基本上具有優勢之程序。In the above liquefaction procedure, the circulating fluid is supplied to the distillation column in a partially liquefied state to extract a heat-balanced liquid product. In order to compress a circulating fluid in an air circulation liquefaction process for forming a circulating fluid, a portion of the high-pressure raw material air is compressed as compared with a nitrogen circulating liquefaction procedure in which a low-pressure and/or medium-pressure nitrogen gas is compressed to form a circulating fluid. The power consumption is less, so it is basically a program with advantages.
然而，當產品液量，特別是液態氮較多時，若為空氣循環液化程序，則供給至中壓塔之原料空氣之液化率會上升，故中壓塔之蒸餾條件會降低，從而變得難以應對。另一方面，氮循環液化程序係將與液體產品相當之液態氮供給至中壓塔之程序，即使於產品液量較多時，中壓塔之蒸餾條件亦不會下降。亦即，於產品液量較少時，動力消耗更少之空氣循環液化程序具有優勢，而於產品液量較多時，則只有氮循環液化程序可加以應對。However, when the amount of liquid in the product, especially liquid nitrogen, is large, if the air circulation liquefaction procedure is performed, the liquefaction rate of the raw material air supplied to the intermediate pressure tower will increase, so the distillation conditions of the intermediate pressure tower will be lowered, thereby becoming Hard to deal with. On the other hand, the nitrogen circulation liquefaction process is a process of supplying liquid nitrogen equivalent to a liquid product to the intermediate pressure column, and even when the product liquid amount is large, the distillation conditions of the intermediate pressure column are not lowered. That is, when the product volume is small, the air circulation liquefaction process with less power consumption has an advantage, and when the product liquid amount is large, only the nitrogen circulation liquefaction program can cope with it.
又，已知有將空氣循環程序用於單精餾塔程序之程序(例如，參照專利文獻2、3、4)。該等程序均係使與單精餾塔之運轉壓力相同程度之原料空氣的一部分循環而升溫至常溫後，導入至原料空氣壓縮機，將其與自外部導入之原料空氣一併壓縮，藉此使程序循環。該等在所循環之原料空氣中不含水蒸氣或二氧化碳，但循環空氣亦成為使前處理裝置循環之程序，因此存在前處理吸附裝置被過度大型化之浪費。Further, a procedure for applying an air circulation program to a single rectification column program is known (for example, refer to Patent Documents 2, 3, and 4). In the above-mentioned procedures, a part of the raw material air which is the same as the operating pressure of the single rectification column is circulated and heated to normal temperature, and then introduced into the raw material air compressor, and compressed together with the raw material air introduced from the outside. Loop the program. These materials do not contain water vapor or carbon dioxide in the circulating raw material air, but the circulating air also becomes a procedure for circulating the pretreatment device, so there is a waste of excessively large size of the pretreatment adsorption device.
此外，亦知有將空氣循環液化程序用於複式精餾塔程序之程序(例如，參照專利文獻5、6)。例如，原料空氣經壓縮機升壓至460 kPa(錶壓，以下記作kPaG)加以純化後，與經膨脹渦輪處理之循環空氣之一部分一併導入至循環空氣壓縮機，升壓至必須之壓力。該等循環空氣經熱交換器冷卻至既定溫度後，被導入至膨脹渦輪，產生裝置所需之寒冷。經膨脹渦輪處理之循環空氣之一部分被導入至中壓塔，剩餘部分則與原料空氣一併被導入至循環壓縮機。於該程序中，中壓塔之運轉壓力約為480 kPaG，成為與膨脹渦輪噴出壓力、前處理裝置運轉壓力相同之程度。Further, a procedure for applying an air circulation liquefaction program to a duplex distillation column program is also known (for example, refer to Patent Documents 5 and 6). For example, the raw material air is purified by a compressor to 460 kPa (gauge pressure, hereinafter referred to as kPaG), and then introduced into a circulating air compressor together with a part of the circulating air treated by the expansion turbine, and is pressurized to a necessary pressure. . The circulating air is cooled to a predetermined temperature by a heat exchanger and introduced into the expansion turbine to produce the cold required for the apparatus. A portion of the circulating air treated by the expansion turbine is introduced to the intermediate pressure tower, and the remainder is introduced to the recycle compressor together with the raw material air. In this procedure, the operating pressure of the intermediate pressure column is approximately 480 kPaG, which is the same as the operating pressure of the expansion turbine and the operating pressure of the pretreatment unit.
又，亦知有一種提取氧氣產品之空氣液化分離裝置，能夠變更所提取之液態氧量比之程序(例如，參照專利文獻7、8)，例如，使來自中壓塔之流體導入前處理設備之後流而與原料空氣一併升壓。又，亦知有利用壓縮機，將來自中壓塔之流體與原料空氣一併壓縮至高於中壓塔之運轉壓力的程序(例如，參照專利文獻9)。但是，於該程序中，亦在冷卻裝置、前處理吸附裝置中對循環流體進行處理，因此該等裝置中需要許多處理能力。Further, there is also known an air liquefaction separation apparatus for extracting an oxygen product, which is capable of changing the ratio of the extracted liquid oxygen amount (for example, refer to Patent Documents 7 and 8), for example, introducing a fluid from an intermediate pressure tower into a pretreatment apparatus. After that, it flows and is boosted together with the raw material air. Further, it is also known that a compressor is used to compress a fluid from an intermediate pressure column together with raw material air to an operating pressure higher than that of the intermediate pressure column (for example, see Patent Document 9). However, in this procedure, the circulating fluid is also processed in the cooling device, the pretreatment adsorption device, and thus many processing capabilities are required in such devices.
[專利文獻1]日本專利第3213846號公報[Patent Document 1] Japanese Patent No. 3213846
[專利文獻2]日本專利特公昭56-034787號公報[Patent Document 2] Japanese Patent Publication No. Sho 56-034787
[專利文獻3]日本專利特公昭60-044584號公報[Patent Document 3] Japanese Patent Publication No. Sho 60-044584
[專利文獻4]日本專利實開昭54-095552號公報[Patent Document 4] Japanese Patent Publication No. Sho 54-095552
[專利文獻5]日本專利特開平06-159929號公報[Patent Document 5] Japanese Patent Laid-Open No. Hei 06-159929
[專利文獻6]日本專利特開平06-159930號公報[Patent Document 6] Japanese Patent Laid-Open No. Hei 06-159930
[專利文獻7]日本專利特開平10-054657號公報[Patent Document 7] Japanese Patent Laid-Open No. Hei 10-054657
[專利文獻8]日本專利特開平10-054658號公報[Patent Document 8] Japanese Patent Laid-Open No. Hei 10-054658
[專利文獻9]日本專利特開平06-300435號公報[Patent Document 9] Japanese Patent Laid-Open No. 06-300435
如上所述，作為液化程序已提出有多種提案，空氣循環液化程序係以改善程序上之效率為主要目的，但就改善裝置價格方面而言尚不充分。As described above, various proposals have been made as a liquefaction program, and the air circulation liquefaction procedure is mainly aimed at improving the efficiency of the procedure, but it is not sufficient in terms of improving the price of the apparatus.
因此，本發明之目的在於提供一種可使至少提取液態氧作為產品之空氣循環液化程序中的裝置價格降低之空氣液化分離方法及裝置。Accordingly, it is an object of the present invention to provide an air liquefaction separation method and apparatus for reducing the cost of a device in an air circulation liquefaction process in which at least liquid oxygen is extracted as a product.
為達成上述目的，本發明之第1構成係一種空氣液化分離方法，其係藉由利用中壓塔及低壓塔，對經壓縮、純化、冷卻之原料空氣進行低溫蒸餾而至少提取液態氧作為產品者，並包含以下步驟：原料空氣壓縮步驟，將原料空氣之總量升壓至高於上述中壓塔之運轉壓力之第1設定壓力，而形成升壓原料空氣；吸附純化步驟，自該升壓原料空氣吸附去除雜質，而形成升壓純化空氣；循環空氣合流步驟，使該升壓純化空氣與後述之升壓回流空氣合流而形成循環空氣；冷卻步驟，使將該循環空氣一分為二之第1分流空氣，冷卻至第1設定溫度而形成中壓塔導入空氣，使第2分流空氣冷卻至高於上述第1設定溫度之第2設定溫度，而形成膨脹用空氣；膨脹步驟，藉由使該膨脹用空氣絕熱膨脹至低於上述第1設定壓力之第2設定壓力，而形成低溫空氣；導入步驟，將該低溫空氣之一部分導入至上述中壓塔；升溫步驟，使該低溫空氣之剩餘部分恢復溫度而形成回流空氣；循環壓縮步驟，使該回流空氣升壓而形成上述升壓回流空氣；以及另一導入步驟，將上述中壓塔導入空氣導入上述中壓塔。In order to achieve the above object, a first aspect of the present invention is an air liquefaction separation method which utilizes a medium pressure column and a low pressure column to perform low temperature distillation of compressed, purified, and cooled raw material air to extract at least liquid oxygen as a product. And comprising the steps of: a raw material air compression step of boosting the total amount of the raw material air to a first set pressure higher than the operating pressure of the intermediate pressure tower to form a pressurized raw material air; and an adsorption purification step from the boosting step The raw material air adsorbs to remove impurities to form pressurized purified air; the circulating air combining step causes the pressurized purified air to merge with the pressurized return air described later to form circulating air; and the cooling step divides the circulating air into two The first split air is cooled to a first set temperature to form an intermediate pressure tower introduction air, and the second split air is cooled to a second set temperature higher than the first set temperature to form an expansion air; and the expansion step is performed by The expansion air is adiabatically expanded to a second set pressure lower than the first set pressure to form a low temperature air; and the introduction step is performed to lower the temperature One part of the gas is introduced into the above-mentioned intermediate pressure tower; a temperature increasing step is performed to restore the remaining portion of the low temperature air to form a return air; a cyclic compression step is performed to pressurize the return air to form the boosted return air; and another introduction step Introducing the above-mentioned intermediate pressure tower into the above-mentioned intermediate pressure tower.
又，本發明之第2構成係一種空氣液化分離方法，其係藉由利用中壓塔及低壓塔，對經壓縮、純化、冷卻之原料空氣進行低溫蒸餾而至少提取液態氧作為產品者，並包含以下步驟：原料空氣壓縮步驟，將原料空氣之總量升壓至高於上述中壓塔之運轉壓力之第1設定壓力，而形成升壓原料空氣；吸附純化步驟，自該升壓原料空氣吸附去除雜質，而形成升壓純化空氣；循環空氣合流步驟，使該升壓純化空氣與後述之升壓回流空氣合流，而形成循環空氣；冷卻步驟，使將該循環空氣一分為三之第1分流空氣冷卻至第1設定溫度，而形成中壓塔導入空氣，使第2分流空氣冷卻至高於上述第1設定溫度之第2設定溫度，而形成冷膨脹用空氣，進而使第3分流空氣冷卻至高於上述第2設定溫度之第3設定溫度，而形成熱膨脹用空氣；第1膨脹步驟，藉由使上述冷膨脹用空氣絕熱膨脹至低於上述第1設定壓力之第2設定壓力，而形成第1低溫空氣；第2膨脹步驟，藉由使上述熱膨脹用空氣絕熱膨脹至上述第2設定壓力，而形成高於上述第1設定溫度之第2低溫空氣；導入步驟，將該第1低溫空氣之一部分導入上述中壓塔；升溫步驟，使該第1低溫空氣之剩餘部分與上述第2低溫空氣恢復溫度而形成回流空氣；循環壓縮步驟，使該回流空氣升壓而形成上述升壓回流空氣；以及另一導入步驟，將上述中壓塔導入空氣導入上述中壓塔。Further, the second configuration of the present invention is an air liquefaction separation method in which at least liquid oxygen is extracted as a product by subjecting a compressed, purified, and cooled raw material air to low temperature distillation by using an intermediate pressure column and a low pressure column. The method comprises the following steps: a raw material air compression step of boosting the total amount of the raw material air to a first set pressure higher than the operating pressure of the intermediate pressure tower to form a pressurized raw material air; and an adsorption purification step for adsorbing air from the pressurized raw material Removing impurities to form pressurized purified air; circulating air mixing step, combining the pressurized purified air with the boosted return air described later to form circulating air; and cooling step to divide the circulating air into three The split air is cooled to the first set temperature, and the intermediate pressure tower is introduced to introduce air, and the second split air is cooled to a second set temperature higher than the first set temperature to form cold expansion air, thereby further cooling the third split air. The air for thermal expansion is formed at a third set temperature higher than the second set temperature; and the first expansion step is performed by using the air for cold expansion. Expanding to a second set pressure lower than the first set pressure to form a first low temperature air; and a second expansion step of adiabatically expanding the thermal expansion air to the second set pressure to form a first higher temperature a second low temperature air having a set temperature; an introduction step of introducing a portion of the first low temperature air into the intermediate pressure column; and a temperature increasing step of recovering a temperature between the remaining portion of the first low temperature air and the second low temperature air to form return air; a cyclic compression step of increasing the reflux air to form the boosted return air; and another introducing step of introducing the intermediate pressure column introduction air into the intermediate pressure column.
此外，於上述第1構成或第2構成中，包含將上述循環空氣升壓至高於上述第1設定壓力的循環空氣升壓步驟。Further, in the first configuration or the second configuration, the circulating air pressure increasing step of raising the circulating air to be higher than the first set pressure is included.
又，本發明之第3構成係一種空氣液化分離裝置，其係藉由利用中壓塔及低壓塔，對經壓縮、純化、冷卻之原料空氣進行低溫蒸餾，而至少提取液態氧作為產品者，且該裝置包含：原料空氣壓縮機，其將原料空氣之總量升壓至高於上述中壓塔之運轉壓力之第1設定壓力，而形成升壓原料空氣；吸附裝置，其自該升壓原料空氣吸附去除雜質，而形成升壓純化空氣；循環空氣合流管道，其使該升壓純化空氣與後述之升壓回流空氣合流，而形成循環空氣；主熱交換器，其使將該循環空氣一分為二之第1分流空氣，冷卻至第1設定溫度而形成中壓塔導入空氣，使第2分流空氣冷卻至高於上述第1設定溫度之第2設定溫度，而形成膨脹用空氣；膨脹渦輪，其使該膨脹用空氣絕熱膨脹至低於上述第1設定壓力之第2設定壓力，而形成低溫空氣；配管，其將該低溫空氣之一部分導入至上述中壓塔；循環壓縮機，其使利用上述主熱交換器使該低溫空氣之剩餘部分恢復溫度而成之回流空氣升壓，而形成上述升壓回流空氣；以及另一配管，其將上述中壓塔導入空氣導入至上述中壓塔。Further, the third aspect of the present invention is an air liquefaction separation apparatus which performs low-temperature distillation of compressed, purified, and cooled raw material air by using an intermediate pressure tower and a low pressure column, and at least extracts liquid oxygen as a product. And the apparatus comprises: a raw material air compressor that boosts the total amount of the raw material air to a first set pressure higher than the operating pressure of the intermediate pressure tower to form a pressurized raw material air; and an adsorption device from which the raw material is pressurized The air adsorbs to remove impurities to form a boosted purified air; the circulating air merged pipe combines the boosted purified air with the boosted return air described later to form circulating air; the main heat exchanger, which makes the circulating air Dividing into two first split air, cooling to a first set temperature to form an intermediate pressure tower introduction air, and cooling the second split air to a second set temperature higher than the first set temperature to form expansion air; expansion turbine And aerating the expansion air to a second set pressure lower than the first set pressure to form a low temperature air; and piping, the part of the low temperature air Introduced to the intermediate pressure column; a circulation compressor that pressurizes the return air obtained by recovering the remaining portion of the low temperature air by the main heat exchanger to form the boosted return air; and another pipe The intermediate pressure column introduction air is introduced into the above intermediate pressure column.
此外，本發明之第4構成係一種空氣液化分離裝置，其係藉由利用中壓塔及低壓塔，對經壓縮、純化、冷卻之原料空氣進行低溫蒸餾而至少提取液態氧作為產品者，且該分離裝置包含：原料空氣壓縮機，其將原料空氣之總量升壓至高於上述中壓塔之運轉壓力之第1設定壓力，而形成升壓原料空氣；吸附裝置，其自該升壓原料空氣吸附去除雜質，而形成升壓純化空氣；循環空氣合流管道，其使該升壓純化空氣與後述之升壓回流空氣合流，而形成循環空氣；主熱交換器，其使將該循環空氣一分為三之第1分流空氣，冷卻至第1設定溫度而形成中壓塔導入空氣，使第2分流空氣冷卻至高於上述第1設定溫度之第2設定溫度，而形成冷膨脹用空氣，進而使第3分流空氣冷卻至高於上述第2設定溫度之第3設定溫度，而形成熱膨脹用空氣；冷膨脹渦輪，其使上述冷膨脹用空氣絕熱膨脹至低於上述第1設定壓力之第2設定壓力，而形成第1低溫空氣；熱膨脹渦輪，其使上述熱膨脹用空氣絕熱膨脹至上述第2設定壓力，而形成第2低溫空氣；配管，其將上述第1低溫空氣之一部分導入至上述中壓塔；循環壓縮機，其使利用上述主熱交換器，使該第1低溫空氣之剩餘部分與上述第2低溫空氣，恢復溫度而成之回流空氣升壓，而形成上述升壓回流空氣；以及另一配管，其將上述中壓塔導入空氣導入至上述中壓塔。Further, the fourth aspect of the present invention is an air liquefaction separation apparatus which uses at least an intermediate pressure tower and a low pressure column to perform low-temperature distillation of compressed, purified, and cooled raw material air to extract at least liquid oxygen as a product, and The separating apparatus includes: a raw material air compressor that boosts a total amount of raw material air to a first set pressure higher than an operating pressure of the intermediate pressure tower to form a pressurized raw material air; and an adsorption device from which the raw material is pressurized The air adsorbs to remove impurities to form a boosted purified air; the circulating air merged pipe combines the boosted purified air with the boosted return air described later to form circulating air; the main heat exchanger, which makes the circulating air Dividing into three first split air, cooling to a first set temperature to form an intermediate pressure tower introduction air, and cooling the second split air to a second set temperature higher than the first set temperature to form a cold expansion air, and further Cooling the third split air to a third set temperature higher than the second set temperature to form air for thermal expansion, and a cold expansion turbine for emptying the cold expansion Adiabatic expansion to a second set pressure lower than the first set pressure to form a first low temperature air; and a thermal expansion turbine that adiabatically expands the thermal expansion air to the second set pressure to form a second low temperature air; And introducing a part of the first low temperature air to the intermediate pressure tower; and a circulation compressor that restores a temperature between the remaining portion of the first low temperature air and the second low temperature air by using the main heat exchanger The return air is boosted to form the boosted return air; and another pipe is introduced to introduce the intermediate pressure tower into the intermediate pressure column.
另外，於上述第3構成或第4構成中，包含使上述循環空氣升壓至高於上述第1設定壓力之循環空氣壓縮機，上述循環空氣升壓機係設置於上述膨脹渦輪之膨脹渦輪制動鼓風機(blower)，且利用鼓風機、發電機、油壓泵中之任一者進行上述膨脹渦輪之制動。Further, the third or fourth configuration includes a circulating air compressor that boosts the circulating air to be higher than the first set pressure, and the circulating air booster is provided in an expansion turbine brake blower of the expansion turbine. (blower), and braking of the expansion turbine is performed by any one of a blower, a generator, and a hydraulic pump.
根據本發明，將先前升壓至與中壓塔之運轉壓力相對應之壓力的原料空氣之總量，升壓至高於中壓塔之運轉壓力之第1設定壓力，例如，中壓塔之運轉壓力的至少1.5倍左右之壓力，並於此狀態下，吸附去除原料空氣中所含之水蒸氣、二氧化碳等雜質，故與習知之一般的空氣液化分離裝置相比，可使吸附裝置及其周邊之配管小型化。又，原料空氣中所含之水蒸氣之分壓相對降低，因此可降低用以吸附去除水分之吸附劑必要量，並且亦可降低吸附劑之再生所需之能量。因此，能夠以與習知相同程度之動力消耗降低裝置價格等。According to the present invention, the total amount of the raw material air previously pressurized to the pressure corresponding to the operating pressure of the intermediate pressure column is boosted to a first set pressure higher than the operating pressure of the intermediate pressure column, for example, the operation of the intermediate pressure column The pressure is at least about 1.5 times the pressure, and in this state, the water vapor, carbon dioxide and the like contained in the raw material air are adsorbed and removed, so that the adsorption device and its periphery can be compared with the conventional air liquefaction separation device. The piping is miniaturized. Further, since the partial pressure of the water vapor contained in the raw material air is relatively lowered, the necessary amount of the adsorbent for adsorbing and removing moisture can be reduced, and the energy required for the regeneration of the adsorbent can also be reduced. Therefore, it is possible to reduce the price of the device or the like with the same power consumption as conventionally.
圖1之第1形態例所示之空氣液化分離裝置，係藉由利用中壓塔11及低壓塔12，對經壓縮、純化、冷卻之原料空氣進行低溫蒸餾，而提取液態氧LO2、液態粗氬LAr及液態氮LN2作為液體產品，並且提取氧氣GO2及氮氣GN2作為氣體產品者，且包含原料空氣壓縮機13、吸附裝置14、循環壓縮機15、主熱交換器16、膨脹渦輪17、主冷凝器18、粗氬塔19、氬冷凝器20、過冷器21作為主要構成機器。In the air liquefaction separation apparatus shown in the first embodiment of Fig. 1, the medium pressure tower 11 and the low pressure column 12 are used to perform low temperature distillation of the compressed, purified, and cooled raw material air to extract liquid oxygen LO 2 and liquid. Crude argon LAr and liquid nitrogen LN 2 are used as liquid products, and oxygen GO 2 and nitrogen GN 2 are extracted as gas products, and include raw material air compressor 13, adsorption device 14, circulation compressor 15, main heat exchanger 16, expansion The turbine 17, the main condenser 18, the crude argon column 19, the argon condenser 20, and the subcooler 21 are main components.
首先，將原料空氣之總量導入至利用原料空氣壓縮機13升壓至高於中壓塔11之運轉壓力之第1設定壓力，而形成升壓原料空氣的原料空氣壓縮步驟。升壓原料空氣係於藉由冷卻器13a加以冷卻，且藉由除水器(drain separator)13b分離冷凝水之後，導入至用以進行吸附純化步驟之吸附裝置14。於吸附裝置14中，使原料空氣中所含之水蒸氣或二氧化碳等雜質，吸附於吸附劑而加以去除，升壓原料空氣經純化而成為升壓純化空氣。該升壓純化空氣經冷卻器14a加以冷卻後，通過用以構成循環空氣合流管道51之一個配管51a，與自循環壓縮機15噴出至另一個合流管道，即，配管51b之升壓回流空氣合流，而進行循環空氣合流步驟，從而成為於配管51c中流動之循環空氣。First, the total amount of the raw material air is introduced into the raw material air compression step of raising the raw material air by the raw air compressor 13 to a first set pressure higher than the operating pressure of the intermediate pressure column 11. The pressurized raw material air is cooled by the cooler 13a, and after the condensed water is separated by a drain separator 13b, it is introduced to the adsorption device 14 for performing the adsorption purification step. In the adsorption device 14, impurities such as water vapor or carbon dioxide contained in the raw material air are adsorbed to the adsorbent and removed, and the pressurized raw material air is purified to be pressurized purified air. The boosted purified air is cooled by the cooler 14a, and then ejected from the recirculation compressor 15 to the other confluent pipe, that is, the pressurized return air of the pipe 51b, through one pipe 51a constituting the circulating air joining pipe 51. Then, the circulating air joining step is performed to become the circulating air flowing in the pipe 51c.
配管51c之循環空氣被一分為二成為配管52之第1分流空氣與配管53之第2分流空氣後，導入至用以進行冷卻步驟之主熱交換器16。第1分流空氣經主熱交換器16冷卻至第1設定溫度，並自主熱交換器16之冷端導出至配管54，而成為中壓塔導入空氣。該中壓塔導入空氣，係藉由閥31減壓至與中壓塔11之運轉壓力相對應之壓力，且以大部分經液化之狀態，自配管55導入至中壓塔11之下部。The circulating air of the piping 51c is divided into two, which are the first divided air of the piping 52 and the second divided air of the piping 53, and then introduced into the main heat exchanger 16 for performing the cooling step. The first split air is cooled to the first set temperature by the main heat exchanger 16, and the cold end of the main heat exchanger 16 is led to the pipe 54 to be introduced into the intermediate pressure tower. The medium pressure tower introduces air to a pressure corresponding to the operating pressure of the intermediate pressure column 11 by the valve 31, and is introduced from the piping 55 to the lower portion of the intermediate pressure column 11 in a state of being mostly liquefied.
配管53之第2分流空氣，係藉由利用主熱交換器16所進行之冷卻步驟，冷卻至高於上述第1設定溫度之第2設定溫度，並於抵達至主熱交換器16的冷端之前被抽出至配管56而成為膨脹用空氣，並被導入至膨脹渦輪17。膨脹用空氣，係藉由膨脹渦輪17，進行絕熱膨脹至低於上述第1設定壓力之第2設定壓力之膨脹步驟，而成為配管57之低溫空氣。該低溫空氣自配管57分流至配管58與配管59，分流至配管59之低溫空氣，係經由閥32而作為上升氣體自配管60導入至中壓塔11之下部。The second split air of the pipe 53 is cooled to a second set temperature higher than the first set temperature by a cooling step by the main heat exchanger 16, and before reaching the cold end of the main heat exchanger 16 The air is taken out to the pipe 56 to be expanded air, and is introduced into the expansion turbine 17 . The expansion air is a low-temperature air which is adiabatically expanded to a second set pressure lower than the first set pressure by the expansion turbine 17, and becomes a low-temperature air of the pipe 57. The low-temperature air is branched from the piping 57 to the piping 58 and the piping 59, and the low-temperature air branched into the piping 59 is introduced into the lower portion of the intermediate pressure tower 11 as a rising gas from the piping 60 via the valve 32.
分流至上述配管58之低溫空氣之剩餘部分，導入至主熱交換器16之冷端而進行升溫步驟，並與上述第1分流空氣及第2分流空氣進行熱交換，而使各分流空氣冷卻至既定溫度，並且自身溫度恢復至常溫附近，從而成為配管61之回流空氣。該回流空氣被抽吸至循環壓縮機15而進行循環壓縮步驟，升壓至與上述升壓純化空氣相對應之壓力後，噴出至上述配管51b而與上述配管51a之升壓純化空氣合流，從而成為配管51c之上述循環空氣。The remaining portion of the low-temperature air branched into the pipe 58 is introduced into the cold end of the main heat exchanger 16 to perform a temperature rising step, and exchanges heat with the first split air and the second split air to cool each of the split air to The temperature is set to a predetermined temperature, and the temperature of the self returns to the vicinity of the normal temperature, thereby becoming the return air of the pipe 61. The return air is sucked into the circulation compressor 15 to perform a cyclic compression step, and is pressurized to a pressure corresponding to the pressurized purified air, and then discharged to the pipe 51b to merge with the pressurized purified air of the pipe 51a. The above-mentioned circulating air of the pipe 51c is obtained.
自配管55及配管60導入至中壓塔11之下部的原料空氣，係藉由該中壓塔11中之蒸餾操作，而分離成中壓塔頂部之中壓富氮氣體(nitrogen-rich gas)與中壓塔底部之富氧液(oxygen-rich liquid)。富氧液係自中壓塔底部被抽出至配管62，藉由過冷器21加以冷卻後，分流至配管63及配管64，配管64之富氧液係經閥33而減壓至與低壓塔12之運轉壓力相對應之壓力後，通過配管65作為回流液而導入至低壓塔12之中間部。The raw material air introduced into the lower portion of the intermediate pressure column 11 from the piping 55 and the piping 60 is separated into the nitrogen-rich gas at the top of the intermediate pressure column by the distillation operation in the intermediate pressure column 11. And an oxygen-rich liquid at the bottom of the medium pressure column. The oxygen-rich liquid is extracted from the bottom of the intermediate pressure column to the piping 62, cooled by the subcooler 21, and then branched to the piping 63 and the piping 64. The oxygen-rich liquid of the piping 64 is depressurized to the low pressure tower via the valve 33. After the pressure corresponding to the operating pressure of 12, the piping 65 is introduced as a reflux liquid to the intermediate portion of the low pressure column 12.
又，在配管63中流動之富氧液係經閥34減壓後，被導入至設置於粗氬塔19上部的氬冷凝器20。經氬冷凝器20氣化而成之富氧氣體(oxygen-rich gas)，通過配管66作為上升氣體而導入至低壓塔12之中間部。導入至低壓塔12之富氧液及富氧氣體中之氧分，係藉由低壓塔12中之蒸餾操作濃縮於低壓塔底部而成為低壓液態氧。該低壓液態氧之一部分被抽出至配管67，藉由過冷器21加以冷卻後，作為液態氧產品而自配管68提取出來。Further, the oxygen-rich liquid flowing through the pipe 63 is depressurized by the valve 34, and then introduced into the argon condenser 20 provided in the upper portion of the crude argon column 19. The oxygen-rich gas vaporized by the argon condenser 20 is introduced into the intermediate portion of the low pressure column 12 through the pipe 66 as a rising gas. The oxygen-rich liquid and the oxygen-rich gas introduced into the low-pressure column 12 are concentrated in the bottom of the low-pressure column by distillation in the low-pressure column 12 to become low-pressure liquid oxygen. A part of the low-pressure liquid oxygen is taken out to the pipe 67, cooled by the subcooler 21, and extracted from the pipe 68 as a liquid oxygen product.
上述中壓塔頂部之中壓富氮氣體，係通過配管69而導入至配置於低壓塔底部之主冷凝器18，與上述低壓液態氧進行間接熱交換，使低壓液態氧氣化而形成低壓氧氣，並且自身經液化而成為液態氮。該液態氮之一部分，係通過配管70作為回流液而返回至中壓塔11之上部，液態氮之剩餘部分，係通過配管71而藉由過冷器21加以冷卻後，一部分分流至配管72而作為液態氮產品提取出來。大部分之液態氮，係藉由閥35減壓至與低壓塔12之運轉壓力相對應之壓力後，通過配管73作為回流液而導入至低壓塔12之上部。The nitrogen-rich gas in the top of the intermediate pressure column is introduced into the main condenser 18 disposed at the bottom of the low-pressure column through the pipe 69, and is indirectly heat-exchanged with the low-pressure liquid oxygen to form a low-pressure liquid to form low-pressure oxygen. And it is liquefied to become liquid nitrogen. One part of the liquid nitrogen is returned to the upper portion of the intermediate pressure column 11 through the pipe 70 as a reflux liquid, and the remaining portion of the liquid nitrogen is cooled by the subcooler 21 through the pipe 71, and a part is branched to the pipe 72. Extracted as a liquid nitrogen product. Most of the liquid nitrogen is depressurized by the valve 35 to a pressure corresponding to the operating pressure of the low pressure column 12, and then introduced into the upper portion of the lower pressure column 12 through the pipe 73 as a reflux liquid.
此外，自低壓塔12之中間部，將富含氬之氣體流體(饋入氬)抽出至配管74並導入至粗氬塔19之下部，藉由粗氬塔19中之蒸餾操作，在粗氬塔頂部，使濃縮有氬之粗氬氣體分離，氬濃度下降之液體則於粗氬塔底部分離。該氬濃度下降之液體自粗氬塔底部被抽出至配管75，並作為下降液而返回至低壓塔12之中間部。Further, from the intermediate portion of the lower pressure column 12, an argon-rich gas fluid (feeding argon) is withdrawn to the pipe 74 and introduced to the lower portion of the crude argon column 19, by distillation operation in the crude argon column 19, in the crude argon At the top of the column, the crude argon gas concentrated under argon is separated, and the liquid having a reduced argon concentration is separated at the bottom of the crude argon column. The liquid having the reduced argon concentration is taken out from the bottom of the crude argon column to the pipe 75, and returned to the intermediate portion of the low pressure column 12 as a descending liquid.
粗氬塔頂部之粗氬氣體，係經由配管76而導入至氬冷凝器20，藉由在該氬冷凝器20中與上述富氧液進行熱交換，而液化成為液態粗氬。該液態粗氬之一部分作為液態粗氬產品而自配管77提取出來，剩餘部分之液態粗氬則通過配管78作為回流液而導入至粗氬塔19之上部。The crude argon gas at the top of the crude argon column is introduced into the argon condenser 20 through the pipe 76, and is liquefied into liquid crude argon by heat exchange with the oxygen-rich liquid in the argon condenser 20. One portion of the liquid crude argon is extracted from the pipe 77 as a liquid crude argon product, and the remaining portion of the liquid crude argon is introduced into the upper portion of the crude argon column 19 through the pipe 78 as a reflux.
藉由上述低壓塔12中之蒸餾操作而於低壓塔頂部濃縮之低壓氮氣，係被抽出至配管79而導入至過冷器21，用作上述各液體之冷卻源後，經由配管80而導入至主熱交換器16之冷端。又，經上述主冷凝器18氣化之低壓氧氣一部分被抽出至配管81，而導入至主熱交換器16之冷端，剩餘之大部分低壓氧氣則成為低壓塔12之上升氣體。此外，在低壓塔12內上升之氣體之一部分作為廢氣WG，自低壓塔12之中上部抽出至配管82，成為過冷器21之冷卻源後，被導入至主熱交換器16之冷端。The low-pressure nitrogen gas concentrated at the top of the low-pressure column by the distillation operation in the low-pressure column 12 is taken out to the pipe 79 and introduced into the subcooler 21, and used as a cooling source for each of the liquids, and then introduced into the pipe 80 through the pipe 80. The cold end of the main heat exchanger 16. Further, a part of the low-pressure oxygen vaporized by the main condenser 18 is taken out to the pipe 81, and introduced to the cold end of the main heat exchanger 16, and the remaining majority of the low-pressure oxygen becomes the rising gas of the low-pressure column 12. Further, a part of the gas which rises in the low pressure column 12 is taken out as an exhaust gas WG from the upper portion of the low pressure column 12 to the pipe 82, becomes a cooling source of the subcooler 21, and is introduced to the cold end of the main heat exchanger 16.
該等低壓氮氣、低壓氧氣及廢氣，係與自主熱交換器16之熱端導入之上述各分流空氣進行熱交換，經溫度恢復而升溫至常溫後，低壓氮氣作為氮氣產品自配管83提取出來，低壓氧氣作為氧氣產品自配管84提取出來，廢氣被抽出至配管85後，作為上述吸附裝置14之再生氣體等使用。The low-pressure nitrogen gas, the low-pressure oxygen gas and the exhaust gas are heat-exchanged with the respective split air introduced from the hot end of the main heat exchanger 16, and after the temperature is restored to the normal temperature by the temperature recovery, the low-pressure nitrogen gas is extracted from the pipe 83 as a nitrogen gas product. The low-pressure oxygen is extracted from the pipe 84 as an oxygen product, and the exhaust gas is taken out to the pipe 85, and used as a regeneration gas or the like of the adsorption device 14.
於如上所述而形成之空氣液化分離裝置中，藉由原料空氣壓縮機13將原料空氣加以升壓之升壓原料空氣之第1設定壓力，係設定為高於中壓塔11之運轉壓力之壓力。通常，包含中壓塔11、低壓塔12、主冷凝器18之複式精餾塔中的中壓塔11運轉壓力約為500 kPaG，自配管60導入至中壓塔11之下部的低溫空氣之壓力亦為相同程度，於配管61中流動之回流空氣亦為與中壓塔11之運轉壓力相同程度約500 kPaG，因此，若將使該循環空氣升壓之循環壓縮機15之壓縮比設為1.5～1.8，則成為與循環壓縮機15之噴出壓力相等之升壓原料空氣之壓力，即，第1設定壓力約為750 kPaG(500 kPaG×1.5)～900 kPaG(500 kPaG×1.8)。In the air liquefaction separation apparatus formed as described above, the first set pressure of the pressurized raw material air which is boosted by the raw material air compressor 13 by the raw material air compressor 13 is set to be higher than the operating pressure of the intermediate pressure column 11. pressure. Generally, the intermediate pressure column 11 in the double rectification column including the intermediate pressure column 11, the low pressure column 12, and the main condenser 18 has an operating pressure of about 500 kPaG, and the pressure of the low temperature air introduced from the piping 60 to the lower portion of the intermediate pressure column 11 In the same manner, the return air flowing through the pipe 61 is also about 500 kPaG to the same operating pressure as the intermediate pressure column 11, so that the compression ratio of the circulating compressor 15 that raises the circulating air is set to 1.5. ～1.8, the pressure of the pressurized raw material air equal to the discharge pressure of the recycle compressor 15, that is, the first set pressure is about 750 kPaG (500 kPaG x 1.5) to 900 kPaG (500 kPaG x 1.8).
因此，於本形態例中，自原料空氣去除雜質之吸附裝置14之運轉壓力與習知通常的空氣液化分離裝置之情況相比為1.5倍左右，因此可使吸附裝置14中之吸附器本體或周邊配管小型化，從而可降低裝置價格。亦即，與習知之吸附裝置相比，可縮小吸附裝置14之吸附筒之筒徑，故吸附筒材料價格將降低，且與原料空氣共存(accompany)之水蒸氣量減少，因此可減少吸附去除水蒸氣所需之氧化鋁凝膠量，故可大幅度降低整個吸附裝置之設備成本。又，原料空氣中所含之水蒸氣量減少，因此無需將原料空氣冷卻至低溫，冷卻設備所需之成本亦得到削減。Therefore, in the present embodiment, the operating pressure of the adsorption device 14 for removing impurities from the raw material air is about 1.5 times that of the conventional air liquefaction separation device, so that the adsorber body in the adsorption device 14 or The peripheral piping is miniaturized, thereby reducing the price of the device. That is, compared with the conventional adsorption device, the diameter of the adsorption tube of the adsorption device 14 can be reduced, so that the price of the adsorption tube material is lowered, and the amount of water vapor coexisting with the raw material air is reduced, thereby reducing adsorption removal. The amount of alumina gel required for water vapor can greatly reduce the equipment cost of the entire adsorption unit. Further, since the amount of water vapor contained in the raw material air is reduced, it is not necessary to cool the raw material air to a low temperature, and the cost required for the cooling equipment is also reduced.
於以下所述之本發明之其他形態例之說明中，對於與上述第1形態例所示之空氣液化分離裝置之構成要素相同之構成要素標附相同符號，並省略詳細說明。又，中壓塔、低壓塔之周邊之構成可採用與上述第1形態例相同之構成，故省略該等部分之圖示及說明。In the description of the other embodiments of the present invention, the same components as those of the air liquefaction separation device shown in the first embodiment are denoted by the same reference numerals, and detailed description thereof will be omitted. Further, the configuration of the periphery of the intermediate pressure tower and the low pressure tower can be the same as that of the first embodiment, and the illustration and description of the portions are omitted.
圖2之第2形態例所示之空氣液化分離裝置，係以如下方式而形成：將循環壓縮機15設為具有第1壓縮段15a及第2壓縮段15b之多段壓縮機，使自第1壓縮段15a噴出之升壓回流空氣與升壓純化空氣合流，而形成循環空氣，藉由利用循環壓縮機15之第2壓縮段15b進行循環空氣升壓步驟，而使該循環空氣進一步升壓而形成高壓之循環空氣後，藉由利用膨脹渦輪17之制動鼓風機22進行第2循環空氣升壓步驟，而使該循環空氣進一步升壓至高壓。The air liquefaction separation apparatus shown in the second embodiment of Fig. 2 is formed by forming the circulation compressor 15 as a multi-stage compressor having the first compression stage 15a and the second compression stage 15b. The boosted return air ejected from the compression section 15a merges with the boosted purified air to form circulating air, and the circulating air boosting step is performed by the second compressed section 15b of the circulating compressor 15 to further boost the circulating air. After the high-pressure circulating air is formed, the second circulating air step-up step is performed by the brake blower 22 of the expansion turbine 17, and the circulating air is further pressurized to a high pressure.
亦即，藉由吸附裝置14將已利用原料空氣壓縮機13使總量升壓至第1設定壓力之原料空氣加以純化之升壓純化空氣，係通過循環空氣合流管道51之配管51a，與自第1壓縮段15a噴出、並經後冷卻器(after cooler)冷卻之配管51b的升壓回流空氣合流至配管51c，藉由第2壓縮段15b升壓至高於第1設定壓力而成為高壓之循環空氣。In other words, the pressure-purifying purified air which has been purified by the raw material air compressor 13 to increase the total amount of the raw material air to the first set pressure by the adsorption device 14 is passed through the piping 51a of the circulating air joining pipe 51, and The boosted return air discharged from the first compressed section 15a and cooled by the after cooler is merged into the pipe 51c, and is boosted to a higher pressure than the first set pressure by the second compressed section 15b. air.
自循環壓縮機15噴出之高壓之循環空氣的一部分，係分流至上述配管52，並與上述同樣地，導入至主熱交換器16而冷卻至第1設定溫度，並且經由配管54、閥31、配管55，以大部分經液化之狀態而導入至中壓塔11之下部。A part of the high-pressure circulating air discharged from the circulation compressor 15 is branched to the pipe 52, and is introduced into the main heat exchanger 16 in the same manner as described above, and is cooled to the first set temperature, and is passed through the pipe 54, the valve 31, The piping 55 is introduced to the lower portion of the intermediate pressure tower 11 in a state of being mostly liquefied.
分流至配管53之高壓之循環空氣的剩餘部分，係在導入至膨脹渦輪17之制動鼓風機22而進一步升壓至高壓後，經由配管86導入至主熱交換器16，冷卻至高於第1設定溫度之第2設定溫度，並於抵達至主熱交換器16之冷端之前抽出至配管56，而成為膨脹用空氣，然後導入至膨脹渦輪17。膨脹用空氣，係藉由膨脹渦輪17絕熱膨脹至低於第1設定壓力之第2設定壓力，而成為配管57之低溫空氣。該低溫空氣之一部分係分流至配管59，經由閥32及配管60導入至中壓塔之下部，低溫空氣之剩餘部分係分流至配管58而導入至主熱交換器16之冷端，經溫度恢復而成為配管61之回流空氣，繼而被抽吸至循環壓縮機15之第1壓縮段15a並進行循環。The remaining portion of the high-pressure circulating air that has been branched into the pipe 53 is introduced into the brake blower 22 of the expansion turbine 17 to be further pressurized to a high pressure, and then introduced into the main heat exchanger 16 via the pipe 86 to be cooled to a temperature higher than the first set temperature. The second set temperature is extracted to the pipe 56 before reaching the cold end of the main heat exchanger 16, and is expanded air, and then introduced into the expansion turbine 17. The air for expansion is adiabatically expanded by the expansion turbine 17 to a second set pressure lower than the first set pressure, and becomes the low temperature air of the pipe 57. One part of the low-temperature air is branched to the piping 59, and introduced to the lower portion of the intermediate pressure tower via the valve 32 and the piping 60. The remaining portion of the low-temperature air is branched to the piping 58 and introduced to the cold end of the main heat exchanger 16, and is subjected to temperature recovery. The return air which becomes the piping 61 is then sucked into the 1st compression stage 15a of the circulation compressor 15, and it circulates.
如上所述，藉由循環空氣升壓步驟，使循環空氣升壓而形成更高壓之循環空氣，藉此可提高膨脹渦輪17中之膨脹率，從而可增大寒冷產生量。As described above, by the circulating air pressure increasing step, the circulating air is pressurized to form a higher-pressure circulating air, whereby the expansion ratio in the expansion turbine 17 can be increased, and the amount of cold generation can be increased.
圖3之第3形態例所示之空氣液化分離裝置中，設置有使溫度相對低之上述第2設定溫度之膨脹用空氣(冷膨脹用空氣)絕熱膨脹的冷膨脹渦輪17a、以及使溫度相對於第2設定溫度更高之第3設定溫度之膨脹用空氣(熱膨脹用空氣)絕熱膨脹的熱膨脹渦輪17b，作為進行膨脹步驟之膨脹渦輪；同時分別設置有冷膨脹渦輪制動鼓風機22a及熱膨脹渦輪制動鼓風機22b，以作為兩個膨脹渦輪17a、17b制動之用。In the air liquefaction separation apparatus shown in the third aspect of the present invention, the cold expansion turbine 17a for adiabatically expanding the expansion air (cold expansion air) having the second set temperature at a relatively low temperature is provided, and the temperature is relatively The thermal expansion turbine 17b that adiabatically expands the expansion air (the air for thermal expansion) at the third set temperature higher than the second set temperature, and serves as an expansion turbine that performs the expansion step; and is provided with a cold expansion turbine brake blower 22a and a thermal expansion turbine brake, respectively. The blower 22b is used as a brake for the two expansion turbines 17a, 17b.
與上述第2形態例同樣地，升壓純化空氣與升壓回流空氣合流後，藉由循環壓縮機15之第2壓縮段15b加以升壓而變為高壓之循環空氣，係分流成配管52之第1分流空氣與配管53之第2分流空氣，分流至配管53之第2分流空氣，係藉由冷膨脹渦輪制動鼓風機22a而進一步升壓，並自配管86導入至主熱交換器16，並且以冷卻至上述第2設定溫度的狀態，抽出至配管56而成為冷膨脹用空氣。該冷膨脹用空氣，係藉由利用冷膨脹渦輪17a進行第1膨脹步驟而絕熱膨脹至上述第2設定壓力，從而成為上述第1設定溫度附近之第1低溫空氣。In the same manner as in the second embodiment, the boosted purified air is combined with the boosted return air, and then pressurized by the second compression stage 15b of the recycle compressor 15 to be a high-pressure circulating air, which is branched into a pipe 52. The second split air of the first split air and the pipe 53 and the second split air branched to the pipe 53 are further pressurized by the cold expansion turbine brake blower 22a, and introduced into the main heat exchanger 16 from the pipe 86, and In the state of being cooled to the second set temperature, the pipe 56 is taken out to be the air for cold expansion. The cold expansion air is adiabatically expanded to the second set pressure by the first expansion step by the cold expansion turbine 17a, and becomes the first low temperature air in the vicinity of the first set temperature.
第1低溫空氣之一部分係自配管57分流至配管59，並經由閥32及配管60導入至中壓塔11之下部，分流至配管58之剩餘部分之第1低溫空氣，係導入至主熱交換器16之冷端而進行溫度恢復，藉此成為配管61之回流空氣，並被抽吸至循環壓縮機15之第1壓縮段15a，並與上述同樣地進行循環。One of the first low-temperature air is branched from the piping 57 to the piping 59, and introduced into the lower portion of the intermediate pressure tower 11 via the valve 32 and the piping 60, and the first low-temperature air branched to the remaining portion of the piping 58 is introduced to the main heat exchange. The temperature is restored by the cold end of the device 16, and the return air of the pipe 61 is sucked into the first compression stage 15a of the circulation compressor 15, and is circulated in the same manner as described above.
另一方面，分流至配管52之第1分流空氣，係藉由熱膨脹渦輪制動鼓風機22b進一步升壓而自配管87導入至主熱交換器16，冷卻至高於上述第2設定溫度之第3設定溫度後，其一部分作為第3分流空氣而分流，並被抽出至配管88而成為熱膨脹用空氣。該熱膨脹用空氣係利用熱膨脹渦輪17b進行第2膨脹步驟，而絕熱膨脹至上述第2設定壓力，藉此成為高於上述第1設定溫度、且低於第3設定溫度之第2低溫空氣，並自與該第2低溫空氣之溫度相對應之位置之配管89導入至主熱交換器16，與溫度恢復中之第1低溫空氣合流、導出至配管61而成為回流空氣，然後在循環壓縮機15中循環。第1分流空氣之剩餘部分，係經主熱交換器16冷卻至第1設定溫度，並經由配管54、閥31、配管55而導入至中壓塔11。On the other hand, the first split air branched to the pipe 52 is further pressurized by the thermal expansion turbine brake blower 22b, introduced into the main heat exchanger 16 from the pipe 87, and cooled to a third set temperature higher than the second set temperature. Thereafter, a part of the air is branched as the third split air, and is taken out to the pipe 88 to become air for thermal expansion. The thermal expansion air is subjected to the second expansion step by the thermal expansion turbine 17b, and is adiabatically expanded to the second set pressure, thereby becoming the second low temperature air that is higher than the first set temperature and lower than the third set temperature. The piping 89 from the position corresponding to the temperature of the second low-temperature air is introduced into the main heat exchanger 16, merges with the first low-temperature air during temperature recovery, and is led to the piping 61 to be return air, and then in the circulation compressor 15 In the loop. The remaining portion of the first split air is cooled to the first set temperature by the main heat exchanger 16, and introduced into the intermediate pressure tower 11 via the pipe 54, the valve 31, and the pipe 55.
如上所述，藉由將膨脹步驟分成熱、冷兩個步驟，可有效率進行利用膨脹渦輪之絕熱膨脹，且可有效地冷卻導入至中壓塔11之原料空氣。As described above, by dividing the expansion step into two steps of heat and cold, the adiabatic expansion by the expansion turbine can be efficiently performed, and the raw material air introduced into the intermediate pressure column 11 can be efficiently cooled.
圖4之第4形態例所示之空氣液化分離裝置，係將上述第3形態例中之循環壓縮機15設為具有第1壓縮段15a、第2壓縮段15b及第3壓縮段15c之多段壓縮機者。藉由循環壓縮機15之第2壓縮段15b而升壓之循環空氣與上述同樣地，分流成配管52之第1分流空氣與配管53之第2分流空氣，第1分流空氣，係藉由熱膨脹渦輪制動鼓風機22b而進一步升壓後，自配管87導入至主熱交換器16，其一部分於上述第3設定溫度下作為第3分流空氣分流至配管88，成為熱膨脹用空氣而導入至熱膨脹渦輪17b。其藉由利用熱膨脹渦輪17b，絕熱膨脹至第2設定壓力而成為與上述相同之第2低溫空氣，並自配管89導入至主熱交換器16進行恢復溫度後，經由配管61在循環壓縮機15中進行循環。In the air liquefaction separation apparatus shown in the fourth embodiment of the present invention, the circulation compressor 15 in the third embodiment is a section including the first compression stage 15a, the second compression stage 15b, and the third compression stage 15c. Compressor. In the same manner as described above, the circulating air pressurized by the second compression section 15b of the circulation compressor 15 is branched into the first split air of the pipe 52 and the second split air of the pipe 53, and the first split air is thermally expanded. After the turbine brake blower 22b is further pressurized, it is introduced into the main heat exchanger 16 from the pipe 87, and a part of the third divided air is branched into the pipe 88 at the third set temperature, and is introduced into the thermal expansion turbine 17b as the air for thermal expansion. . By the thermal expansion turbine 17b, the second set air is adiabatically expanded to the second set pressure, and is introduced into the main heat exchanger 16 from the pipe 89 to recover the temperature, and then the compressor 15 is placed in the circulation compressor 15 via the pipe 61. Loop in.
另一方面，配管53之第2分流空氣，係藉由第3壓縮段15c及冷膨脹渦輪制動鼓風機22a進一步升壓至高壓後，經由配管86被導入至主熱交換器16，並於上述第2設定溫度下被抽出至配管56而成為冷膨脹用空氣，並且藉由冷膨脹渦輪17a絕熱膨脹至第2設定壓力，藉此成為上述第1設定溫度附近之第1低溫空氣。配管57之第1低溫空氣一部分，係自配管59經由閥32及配管60而導入至中壓塔11之下部，剩餘部分之第1低溫空氣係自配管58導入至主熱交換器16，而與上述第2低溫空氣合流，經溫度恢復而成為配管61之回流空氣，繼而被抽吸至循環壓縮機15進行循環。On the other hand, the second split air of the pipe 53 is further pressurized to a high pressure by the third compression stage 15c and the cold expansion turbine brake blower 22a, and then introduced into the main heat exchanger 16 via the pipe 86, and is described above. 2, the temperature is extracted to the pipe 56 to be the cold expansion air, and the cold expansion turbine 17a is adiabatically expanded to the second set pressure, thereby becoming the first low temperature air in the vicinity of the first set temperature. A part of the first low-temperature air of the piping 57 is introduced from the piping 59 to the lower portion of the intermediate pressure tower 11 via the valve 32 and the piping 60, and the remaining first low-temperature air is introduced from the piping 58 to the main heat exchanger 16, and The second low-temperature air merges as a return air of the pipe 61 after the temperature is recovered, and is then sucked into the circulation compressor 15 to be circulated.
圖5之第5形態例所示之空氣液化分離裝置，係設置發電機23代替上述第4形態例中之冷膨脹渦輪制動鼓風機22a，並利用發電機23進行冷膨脹渦輪17a之制動，並且將分流至配管53藉由循環壓縮機15之第3壓縮段15c而升壓之第2分流空氣，保持如此之壓力而自配管90導入至主熱交換器16。如此，作為膨脹渦輪之制動，可採用除鼓風機制動以外之電動機制動或油壓制動。In the air liquefaction separation apparatus shown in the fifth aspect of the present invention, the generator 23 is provided in place of the cold expansion turbine brake blower 22a in the fourth embodiment, and the cold expansion turbine 17a is braked by the generator 23, and The second split air that is boosted by the third compression section 15c of the circulation compressor 15 is branched to the piping 53, and is introduced into the main heat exchanger 16 from the piping 90 while maintaining such pressure. Thus, as the brake of the expansion turbine, motor brake or hydraulic brake other than the blower brake can be employed.
圖6之第6形態例所示之空氣液化分離裝置係以如下方式形成，即，使藉由原料空氣壓縮機13而升壓至高於中壓塔11之運轉壓力之第1設定壓力、且經吸附裝置14純化後之升壓純化空氣，與藉由循環壓縮機15而升壓、進而藉由冷膨脹渦輪制動鼓風機22a及熱膨脹渦輪制動鼓風機22b升壓後之升壓回流空氣合流。The air liquefaction separation apparatus shown in the sixth embodiment of Fig. 6 is formed by raising the pressure to a first set pressure higher than the operating pressure of the intermediate pressure column 11 by the raw material air compressor 13, and The boosted purified air purified by the adsorption device 14 is combined with the boosted return air pressurized by the circulating compressor 15 and further pressurized by the cold expansion turbine brake blower 22a and the thermal expansion turbine brake blower 22b.
亦即，自吸附裝置14導出至配管91之升壓純化空氣，係分流至用以構成循環空氣合流管道之配管92與配管93。另一方面，藉由循環壓縮機15將配管61之回流空氣加以升壓之升壓回流空氣，係分流至朝向冷膨脹渦輪制動鼓風機22a之配管94、以及朝向熱膨脹渦輪制動鼓風機22b之配管95。That is, the pressurized purified air which is taken out from the adsorption device 14 to the pipe 91 is branched to the piping 92 and the piping 93 which constitute the circulating air joining pipe. On the other hand, the step-up return air that boosts the return air of the pipe 61 by the circulation compressor 15 is branched into a pipe 94 that faces the cold expansion turbine brake blower 22a, and a pipe 95 that faces the thermal expansion turbine brake blower 22b.
分流至配管94並藉由冷膨脹渦輪制動鼓風機22a進一步升壓之升壓回流空氣，係通過用以構成循環空氣合流管道之配管96與來自上述配管92之升壓純化空氣合流，並通過配管97而導入至主熱交換器16，經冷卻至第2設定溫度後被抽出至配管56，成為上述冷膨脹用空氣而導入至冷膨脹渦輪17a。The step-up return air which is further pressurized by the cold expansion turbine brake blower 22a is branched into the piping 94, and is merged with the pressurized purified air from the piping 92 through the piping 96 for constituting the circulating air joining duct, and passed through the piping 97. The main heat exchanger 16 is introduced into the main heat exchanger 16 and is cooled to the second set temperature, and then extracted into the pipe 56 to be introduced into the cold expansion turbine 17a.
分流至配管95並藉由熱膨脹渦輪制動鼓風機22b進一步升壓之升壓回流空氣，係通過用以構成循環空氣合流管道之配管98與來自上述配管93之升壓純化空氣合流，並通過配管99而導入至主熱交換器16，其一部分於冷卻至第3設定溫度之階段被抽出至配管88，成為熱膨脹用空氣而導入至熱膨脹渦輪17b，剩餘部分則於冷卻至第1設定溫度後，成為配管54之中壓塔導入空氣而導入至中壓塔11。The step-up return air which is further pressurized by the thermal expansion turbine brake blower 22b is branched into the piping 95, and is connected to the pressurized purified air from the piping 93 through the piping 98 for constituting the circulating air joining duct, and is passed through the piping 99. The main heat exchanger 16 is introduced into the main heat exchanger 16, and a part thereof is drawn to the pipe 88 at the stage of cooling to the third set temperature, and is introduced into the thermal expansion turbine 17b as air for thermal expansion, and the remaining portion is cooled to the first set temperature to become a pipe. The intermediate pressure tower 54 is introduced into the intermediate pressure column 11 by introducing air.
再者，於各形態例中，係列舉了提取液態氧LO2、液態粗氬LAr及液態氮LN2作為液體產品之示例，但亦可應用於僅提取液態氧LO2作為液體產品之空氣液化分離裝置，且亦可應用於提取液態氧LO2與液態粗氬LAr、液態氧LO2與液態氮LN2之組合。又，作為循環壓縮機，可根據吸入壓力、噴出壓力、處理量，使用具有4段以上之壓縮段之壓縮機。Further, in each of the examples, the series of liquid oxygen LO 2 , liquid crude argon LAr and liquid nitrogen LN 2 are taken as liquid products, but can also be applied to air liquefaction which only extracts liquid oxygen LO 2 as a liquid product. The separation device can also be applied to extract a combination of liquid oxygen LO 2 and liquid crude argon LAr, liquid oxygen LO 2 and liquid nitrogen LN 2 . Further, as the circulation compressor, a compressor having a compression stage of four or more stages can be used depending on the suction pressure, the discharge pressure, and the throughput.
其次，說明使用上述第3形態例所示之空氣液化分離裝置，提取液態氧1500 Nm3/h、液態氮1000 Nm3/h及液態氬50 Nm3/h之情況之具體例。再者，[Nm3/h]係表示於0℃、1個大氣壓下換算而得之每小時之流量。Next, a specific example in which liquid 1500 Nm 3 /h, liquid nitrogen 1000 Nm 3 /h, and liquid argon 50 Nm 3 /h are extracted using the air liquefaction separation apparatus shown in the third embodiment will be described. Further, [Nm 3 /h] is an hourly flow rate obtained by conversion at 0 ° C and 1 atm.
首先，將原料空氣(8800 Nm3/h)之總量，係藉由原料空氣壓縮機13升壓至約850 kPaG後，導入至使用有活性氧化鋁凝膠及沸石(zeolite)之吸附裝置14，吸附去除原料空氣中所含之水蒸氣或二氧化碳等雜質並加以純化。經純化之原料空氣(升壓純化空氣)導入至循環壓縮機15之第1壓縮段15a與第2壓縮段15b之間，並與自第1壓縮段15a所噴出之升壓回流空氣(12800 Nm3/h)合流，並藉由第2壓縮段15b升壓至2700 kPaG而成為循環空氣。First, the total amount of raw material air (8800 Nm 3 /h) is pressurized to about 850 kPaG by the raw material air compressor 13, and then introduced into an adsorption device 14 using activated alumina gel and zeolite. The water vapor or carbon dioxide contained in the raw material air is adsorbed and removed and purified. The purified raw material air (boosted purified air) is introduced between the first compression section 15a and the second compression section 15b of the recycle compressor 15 and the boosted return air (12800 Nm) ejected from the first compression section 15a. 3 / h) merges and is boosted to 2700 kPaG by the second compression section 15b to become circulating air.
循環空氣之一部分(第1分流空氣7700 Nm3/h)，係藉由熱膨脹渦輪制動鼓風機22b升壓至4000 kPaG後，導入至主熱交換器16。第1分流空氣之一部分(第3分流空氣4000 Nm3/h)，係於藉由主熱交換器16冷卻至第3設定溫度之階段，自主熱交換器16抽出，並導入至熱膨脹渦輪17b而絕熱膨脹至第2設定壓力，藉此成為第2低溫空氣。第1分流空氣之剩餘部分(3700 Nm3/h)，係藉由主熱交換器16冷卻至第1設定溫度，經閥31減壓至中壓塔對應壓力後，通過配管55而導入至中壓塔11。One part of the circulating air (the first divided air 7700 Nm 3 /h) is boosted to 4000 kPaG by the thermal expansion turbine brake blower 22b, and then introduced into the main heat exchanger 16. One of the first split air (third split air 4000 Nm 3 /h) is at a stage where the main heat exchanger 16 is cooled to the third set temperature, and the main heat exchanger 16 is taken out and introduced into the thermal expansion turbine 17b. The adiabatic expansion expands to the second set pressure, thereby becoming the second low temperature air. The remaining portion of the first split air (3700 Nm 3 /h) is cooled to the first set temperature by the main heat exchanger 16, and is depressurized to a pressure corresponding to the intermediate pressure tower via the valve 31, and then introduced into the medium through the pipe 55. Press tower 11.
循環空氣之剩餘部分(第2分流空氣13900 Nm3/h)，係藉由冷膨脹渦輪制動鼓風機22a升壓至4000 kPaG並導入至主熱交換器16，經主熱交換器16冷卻至第2設定溫度後，導入至冷膨脹渦輪17a而進行絕熱膨脹，藉此成為第1低溫空氣。第1低溫空氣之一部分(8800 Nm3/h)，係導入至主熱交換器16後與上述第2低溫空氣合流，而成為原料空氣(循環空氣)之冷卻源，藉此經溫度恢復而成為回流空氣。第1低溫空氣之剩餘部分(5100 Nm3/h)通過閥32、配管60而導入至中壓塔11之下部。The remaining portion of the circulating air (second split air 13900 Nm 3 /h) is boosted to 4000 kPaG by the cold expansion turbine brake blower 22a and introduced into the main heat exchanger 16, and cooled to the second heat exchanger 16 After the temperature is set, it is introduced into the cold expansion turbine 17a to perform adiabatic expansion, thereby becoming the first low temperature air. One of the first low-temperature air (8800 Nm 3 /h) is introduced into the main heat exchanger 16 and merges with the second low-temperature air to become a cooling source of the raw material air (circulating air), thereby being restored by temperature. Return air. The remaining portion of the first low temperature air (5100 Nm 3 /h) is introduced into the lower portion of the intermediate pressure column 11 through the valve 32 and the pipe 60.
被導入至中壓塔11之原料空氣(來自配管55之3700 Nm3/h、來自配管60之5100 Nm3/h)，係藉由利用中壓塔11、低壓塔12及粗氬塔19進行低溫蒸餾，而成為液態氧1500 Nm3/h、液態氮1000 Nm3/h、液態氬50 Nm3/h之液體產品，氧氣、氮氣之氣體產品以及廢氣。The raw material air (3700 Nm 3 /h from the piping 55 and 5100 Nm 3 /h from the piping 60) introduced into the intermediate pressure tower 11 is performed by using the intermediate pressure tower 11, the low pressure column 12, and the crude argon column 19. Low-temperature distillation, which becomes liquid product of liquid oxygen 1500 Nm 3 /h, liquid nitrogen 1000 Nm 3 /h, liquid argon 50 Nm 3 /h, oxygen gas, nitrogen gas product and exhaust gas.
將在主要配管中流動之氣體液體之流量、溫度、壓力、氧氣組成示於表1，並且將對本實施例中之吸附裝置與習知技術之吸附裝置進行對比之吸附裝置之主要規格示於表2。再者，表2中之活性氧化鋁量以下，係指將習知裝置設為100時之相對值。The flow rate, temperature, pressure, and oxygen composition of the gas liquid flowing in the main piping are shown in Table 1, and the main specifications of the adsorption apparatus which compares the adsorption apparatus of this embodiment with the adsorption apparatus of the prior art are shown in the table. 2. In addition, the amount of activated alumina in Table 2 below is a relative value when the conventional apparatus is set to 100.
11．．．中壓塔11. . . Medium voltage tower
12．．．低壓塔12. . . Low pressure tower
13．．．原料空氣壓縮機13. . . Raw air compressor
13a、14a．．．冷卻器13a, 14a. . . Cooler
13b．．．除水器13b. . . Water remover
14．．．吸附裝置14. . . Adsorption device
15．．．循環壓縮機15. . . Circulating compressor
15a．．．第1壓縮段15a. . . First compression section
15b．．．第2壓縮段15b. . . Second compression section
15c．．．第3壓縮段15c. . . Third compression section
16．．．主熱交換器16. . . Main heat exchanger
17．．．膨脹渦輪17. . . Expansion turbine
17a．．．冷膨脹渦輪17a. . . Cold expansion turbine
17b．．．熱膨脹渦輪17b. . . Thermal expansion turbine
18．．．主冷凝器18. . . Main condenser
19．．．粗氬塔19. . . Crude argon column
20．．．氬冷凝器20. . . Argon condenser
21．．．過冷器twenty one. . . Subcooler
22．．．制動鼓風機twenty two. . . Brake blower
22a．．．冷膨脹渦輪制動鼓風機22a. . . Cold expansion turbine brake blower
22b．．．熱膨脹渦輪制動鼓風機22b. . . Thermal expansion turbine brake blower
23．．．發電機twenty three. . . generator
31～35．．．閥31~35. . . valve
51．．．循環空氣合流管道51. . . Circulating air joining pipe
51a～51c、52～99．．．配管51a～51c, 52～99. . . Piping
圖1係表示本發明之第1形態例的空氣液化分離裝置之系統圖。Fig. 1 is a system diagram showing an air liquefaction separation apparatus according to a first embodiment of the present invention.
圖2係表示本發明之第2形態例的空氣液化分離裝置之主要部分系統圖。Fig. 2 is a system diagram showing the main part of an air liquefaction separation apparatus according to a second embodiment of the present invention.
圖3係表示本發明之第3形態例的空氣液化分離裝置之主要部分系統圖。Fig. 3 is a system diagram showing main parts of an air liquefaction separation apparatus according to a third embodiment of the present invention.
圖4係表示本發明之第4形態例的空氣液化分離裝置之主要部分系統圖。Fig. 4 is a system diagram showing the main part of an air liquefaction separation apparatus according to a fourth embodiment of the present invention.
圖5係表示本發明之第5形態例的空氣液化分離裝置之主要部分系統圖。Fig. 5 is a system diagram showing the main part of an air liquefaction separation apparatus according to a fifth embodiment of the present invention.
圖6係表示本發明之第6形態例的空氣液化分離裝置之主要部分系統圖。Fig. 6 is a system diagram showing the main part of an air liquefaction separation apparatus according to a sixth embodiment of the present invention.
11．．．中壓塔11. . . Medium voltage tower
12．．．低壓塔12. . . Low pressure tower
13．．．原料空氣壓縮機13. . . Raw air compressor
13a、14a．．．冷卻器13a, 14a. . . Cooler
13b．．．除水器13b. . . Water remover
14．．．吸附裝置14. . . Adsorption device
15．．．循環壓縮機15. . . Circulating compressor
16．．．主熱交換器16. . . Main heat exchanger
17．．．膨脹渦輪17. . . Expansion turbine
18．．．主冷凝器18. . . Main condenser
19．．．粗氬塔19. . . Crude argon column
20．．．氬冷凝器20. . . Argon condenser
21．．．過冷器twenty one. . . Subcooler
31～35．．．閥31~35. . . valve
51．．．循環空氣合流管道51. . . Circulating air joining pipe
51a～51c、52～85．．．配管51a～51c, 52～85. . . Piping
Claims (10)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2009173323A JP5643491B2 (en) | 2009-07-24 | 2009-07-24 | Air liquefaction separation method and apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| TW201109602A TW201109602A (en) | 2011-03-16 |
| TWI525298B true TWI525298B (en) | 2016-03-11 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| TW099124121A TWI525298B (en) | 2009-07-24 | 2010-07-22 | Air liquefaction separation method and device |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US20120131951A1 (en) |
| JP (1) | JP5643491B2 (en) |
| KR (1) | KR20120040685A (en) |
| CN (1) | CN102472575B (en) |
| TW (1) | TWI525298B (en) |
| WO (1) | WO2011010630A1 (en) |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9518778B2 (en) * | 2012-12-26 | 2016-12-13 | Praxair Technology, Inc. | Air separation method and apparatus |
| US20150033792A1 (en) * | 2013-07-31 | 2015-02-05 | General Electric Company | System and integrated process for liquid natural gas production |
| US9291389B2 (en) | 2014-05-01 | 2016-03-22 | Praxair Technology, Inc. | System and method for production of argon by cryogenic rectification of air |
| US10337792B2 (en) | 2014-05-01 | 2019-07-02 | Praxair Technology, Inc. | System and method for production of argon by cryogenic rectification of air |
| WO2015187117A1 (en) | 2014-06-02 | 2015-12-10 | Praxair Technology, Inc. | Air separation system and method |
| US9731241B2 (en) * | 2014-06-12 | 2017-08-15 | Air Products And Chemicals, Inc. | Radial flow adsorber ‘U’ configuration |
| US10060673B2 (en) | 2014-07-02 | 2018-08-28 | Praxair Technology, Inc. | Argon condensation system and method |
| US10295252B2 (en) * | 2015-10-27 | 2019-05-21 | Praxair Technology, Inc. | System and method for providing refrigeration to a cryogenic separation unit |
| EP3196574B1 (en) * | 2016-01-21 | 2021-05-05 | Linde GmbH | Process and apparatus for producing pressurized gaseous nitrogen by cryogenic separation of air |
| US10267561B2 (en) * | 2016-06-30 | 2019-04-23 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Apparatus for the production of air gases by the cryogenic separation of air |
| CN109564060B (en) * | 2016-06-30 | 2021-08-13 | 乔治洛德方法研究和开发液化空气有限公司 | Method for producing air gas by cryogenic separation of air |
| US10302356B2 (en) * | 2016-06-30 | 2019-05-28 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for the production of air gases by the cryogenic separation of air |
| CN109642771B (en) * | 2016-06-30 | 2021-07-23 | 乔治洛德方法研究和开发液化空气有限公司 | Method and apparatus for operating an air separation plant |
| US10260802B2 (en) * | 2016-06-30 | 2019-04-16 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Apparatus for operating an air separation plant |
| CN110090514A (en) * | 2018-01-29 | 2019-08-06 | 株式会社田村制作所 | Gas cleaning plant, method for gas purification and delivery heating device |
| CN109855389B (en) * | 2019-01-04 | 2020-11-13 | 曹建喜 | Method for producing liquid oxygen and liquid nitrogen by using LNG cold energy and single-tower rectification process |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1520103A (en) * | 1977-03-19 | 1978-08-02 | Air Prod & Chem | Production of liquid oxygen and/or liquid nitrogen |
| JPS5495552U (en) * | 1977-12-16 | 1979-07-06 | ||
| US4375367A (en) * | 1981-04-20 | 1983-03-01 | Air Products And Chemicals, Inc. | Lower power, freon refrigeration assisted air separation |
| US4715873A (en) * | 1986-04-24 | 1987-12-29 | Air Products And Chemicals, Inc. | Liquefied gases using an air recycle liquefier |
| US4705548A (en) * | 1986-04-25 | 1987-11-10 | Air Products And Chemicals, Inc. | Liquid products using an air and a nitrogen recycle liquefier |
| US5275003A (en) * | 1992-07-20 | 1994-01-04 | Air Products And Chemicals, Inc. | Hybrid air and nitrogen recycle liquefier |
| FR2714721B1 (en) * | 1993-12-31 | 1996-02-16 | Air Liquide | Method and installation for liquefying a gas. |
| JP2875206B2 (en) * | 1996-05-29 | 1999-03-31 | 日本エア・リキード株式会社 | High purity nitrogen production apparatus and method |
| US5678425A (en) * | 1996-06-07 | 1997-10-21 | Air Products And Chemicals, Inc. | Method and apparatus for producing liquid products from air in various proportions |
-
2009
- 2009-07-24 JP JP2009173323A patent/JP5643491B2/en active Active
-
2010
- 2010-07-20 KR KR1020117028238A patent/KR20120040685A/en not_active Application Discontinuation
- 2010-07-20 US US13/386,466 patent/US20120131951A1/en not_active Abandoned
- 2010-07-20 WO PCT/JP2010/062158 patent/WO2011010630A1/en active Application Filing
- 2010-07-20 CN CN201080032477.8A patent/CN102472575B/en active Active
- 2010-07-22 TW TW099124121A patent/TWI525298B/en active
Also Published As
| Publication number | Publication date |
|---|---|
| CN102472575A (en) | 2012-05-23 |
| CN102472575B (en) | 2014-11-05 |
| JP2011027318A (en) | 2011-02-10 |
| JP5643491B2 (en) | 2014-12-17 |
| TW201109602A (en) | 2011-03-16 |
| WO2011010630A1 (en) | 2011-01-27 |
| US20120131951A1 (en) | 2012-05-31 |
| KR20120040685A (en) | 2012-04-27 |
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