TW201903342A - 用於獲得一或多種空氣產品之方法及空氣分離廠 - Google Patents
用於獲得一或多種空氣產品之方法及空氣分離廠 Download PDFInfo
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- TW201903342A TW201903342A TW107118919A TW107118919A TW201903342A TW 201903342 A TW201903342 A TW 201903342A TW 107118919 A TW107118919 A TW 107118919A TW 107118919 A TW107118919 A TW 107118919A TW 201903342 A TW201903342 A TW 201903342A
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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
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
- F25J3/04915—Combinations of different material exchange elements, e.g. within different columns
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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
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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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
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- 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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
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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
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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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
- F25J3/04109—Arrangements of compressors and /or their drivers
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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
- F25J3/04351—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 nitrogen
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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.
- F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
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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
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- 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
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- 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
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- 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
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
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- F25J3/04642—Recovering noble gases from air
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- 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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- F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
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- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
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- 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
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- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/54—Oxygen production with multiple pressure O2
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- 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
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Abstract
本發明提出使用空氣分離廠而獲得空氣產品的方法,該空氣分離廠具有精餾管柱系統,其包含高壓管柱及低壓管柱;及具有主熱交換器及主空氣壓縮器,在該主空氣壓縮器中將供應至該精餾管柱系統之總空氣壓縮至第一壓力,且在第二壓力下將氣態富氮流體自該高壓管柱移除且在不預先液化之情況下以該氣態形式升溫。其限制條件為將第一部分數量之該氣態富氮流體升溫至-150至-100℃之第一溫度,在此溫度下供應至增壓器,且藉由使用該增壓器進一步壓縮至第三壓力,且該第一部分數量升溫至高於該第一溫度之第二溫度且自該空氣分離廠永久性地排出。
Description
本發明係關於一種用於獲得一或多種空氣產品的方法且關於根據從屬申請專利範圍之前言的空氣分離廠。
藉由在空氣分離廠中低溫分離空氣產生呈液態或氣態之空氣產品為已知的且描述於例如H.-W. Häring (編), Industrial Gases Processing, Wiley-VCH, 2006, 特定而言章節2.2.5, 「Cryogenic Rectification」中。
空氣分離廠具有精餾管柱系統,其可例如呈兩個管柱系統之形式,特定而言典型的林德雙管柱系統(Linde double-column system),以及三個或多個管柱系統。除用於獲得呈液態及/或氣態之氮氣及/或氧氣的精餾管柱,亦即用於氮氣-氧氣分離之精餾管柱以外,亦有可能得到用於獲得其他空氣組分,特定而言惰性氣體氪氣、氙氣及/或氬氣之精餾管柱。
在不同壓力位準下操作所提及之精餾管柱系統之精餾管柱。雙管柱系統具有所謂的高壓管柱(亦稱為壓力管柱,中壓管柱或下部管柱)及所謂的低壓管柱(亦稱為上部管柱)。高壓管柱之壓力位準為例如4至6巴,較佳大約5.5巴。在例如1.3至1.7巴,較佳大約1.5巴之壓力位準下操作低壓管柱。此處及下文指定之壓力位準在各情況中為分別提及之管柱頂部處的絕對壓力。所提及之值僅作為實例給出,其可在需要時改變。
所謂的主空氣壓縮器/增壓空氣壓縮器(MAC-BAC)方法或所謂的高氣壓(HAP)方法可用於空氣分離。主空氣壓縮器/增壓空氣壓縮器方法為相當習知之方法,而高氣壓方法最近越來越多地被用作替代方案。
藉由將供應至精餾管柱系統之總饋入空氣數量之僅一部分壓縮至顯著地高於高壓管柱之壓力位準(亦即高至少3、4、5、6、7、8、9或10巴)之壓力位準的事實來區分主空氣壓縮器/增器空氣壓縮器方法。將饋入空氣數量之另外的部分僅壓縮至高壓管柱之壓力位準或壓縮至與高壓管柱之壓力位準相差超過1至2巴的壓力位準,且在此較低壓力位準下將其饋入至高壓管柱中。藉由Häring (參見上文)在圖2.3A中展示主空氣壓縮器/增壓空氣壓縮器方法之一實例。
在高氣壓方法之情況下,在另一方面,將供應至精餾管柱系統之總饋入空氣數量壓縮至顯著地高於高壓管柱之壓力位準(亦即高至少3、4、5、6、7、8、9或10巴)之壓力位準。壓力差可為例如至多14、16、18或20巴。例如自EP 2 980 514 A1及EP 2 963 367 A1已知高氣壓方法。
本發明用於特定而言具有所謂的內部壓縮(IC)之空氣分離廠之情況中。此涉及形成至少一種產品,該產品藉由自精餾管柱系統移除低溫液體,使其經受壓力增加且藉由使其升溫而將其轉換為氣態或超臨界狀態藉助於空氣分離系統提供。舉例而言,以此方式,可產生經內部壓縮之氣態氧氣(GOX IV、GOX IC)或氮氣(GAN IV、GAN IC)。內部壓縮提供了一系列優於替代地同樣可能的外部壓縮之優點,且例如由Häring (參見上文), 章節2.2.5.2, 「Internal Compression」解釋。內部壓縮方法亦揭示於例如US 2004/0221612 A1及US 5,475,980 A中。
由於顯著地低成本及類似效率,高氣壓方法可表示習知主空氣壓縮器/增壓空氣壓縮器方法的有利替代方案。然而,此不在所有情況下適用。因此,本發明解決使得有可能至少在一些此等情況下有利地使用高氣壓方法的問題。
此問題由獲得一或多種空氣產品之方法及具有從屬申請專利範圍之特徵的空氣分離廠來解決。組態分別為從屬申請專利範圍及以下描述之主題。
首先,以下為本發明之原理中之一些之解釋及用於描述本發明之術語之定義。
在本申請案之上下文中,將「饋入空氣數量」或簡稱「饋入空氣」理解為意謂全部供應至空氣分離廠之精餾管柱系統的空氣,且因此供應至精餾管柱系統之所有空氣。如上文已解釋,在主空氣壓縮器/增壓空氣壓縮器方法中,將相應饋入空氣數量之僅一部分壓縮至顯著地高於高壓管柱之壓力位準的壓力位準。在另一方面,在高氣壓方法中,將總饋入空氣數量壓縮至此高壓水平。對於與主空氣壓縮器/增壓空氣壓縮器及高氣壓方法有關之術語「顯著地」的含義,應參考上文給出之解釋。
在此將「低溫」液體理解為意謂沸點顯著地低於環境溫度,例如在-50℃下或更低,特定而言在-100℃下或更低的液態介質。低溫液體之實例為液態空氣、液態氧、液態氮、液態氬或在所提及之化合物中富含之液體。
對於用於空氣分離廠中之裝置及設備,應參考專業文獻,諸如Häring (參見上文), 特定而言章節2.2.5.6 「Apparatus」。出於說明及更清晰界定之目的,以下為相應裝置之態樣中之一些的更詳細解釋。
多級渦輪壓縮器(在此稱為「主空氣壓縮器」)用於空氣分離廠中以用於壓縮饋入空氣數量。渦輪壓縮器之機械建構原則上為熟習此項技術者所已知的。在渦輪壓縮器中,藉助於佈置於渦輪機轉輪或轉軸正上方上之渦輪機刮刀來壓縮待壓縮介質。在該情形中,渦輪壓縮器形成結構單元,然而該結構單元在多級渦輪壓縮器之情況下可具有多個壓縮器級。壓縮器級通常包含轉輪或渦輪機刮刀之相應佈置。所有此等壓縮器級可由公共轉軸驅動。然而,亦可設想在具有不同轉軸之組中驅動壓縮器級,亦有可能藉助於齒輪機制將轉軸彼此連接。
亦藉由饋入至精餾管柱系統中及用於產生空氣產品之總數量之空氣(亦即總饋入空氣)藉由此壓縮器壓縮的事實來區分主空氣壓縮器。相應地,亦可提供「增壓空氣壓縮器」,然而,其中將在主空氣壓縮器中壓縮之僅一部分數量之空氣帶至另外更高的壓力。此亦可形成為渦輪壓縮器。另外的渦輪壓縮器(在本文中亦指增壓器)通常為壓縮部分數量之空氣而提供,但其與主空氣壓縮器或增壓空氣壓縮器相比僅進行壓縮至相對較小程度。在高氣壓方法中亦可存在增壓空氣壓縮器,但此接著自相應地更高壓力位準壓縮部分數量之空氣。
此外,空氣可在空氣分離廠中之數個點處膨脹,出於此目的,尤其可使用呈渦輪膨脹器形式(在本文中亦指「膨脹渦輪機」)的膨脹機器。渦輪膨脹器亦可耦接至渦輪壓縮器且驅動其。若在不具有外部供應能量之情況下,亦即僅藉由一或多個渦輪膨脹器驅動一或多個渦輪壓縮器,術語「渦輪機增壓器」亦用於此類佈置中。在渦輪機增壓器中,渦輪膨脹器(膨脹渦輪機)及渦輪壓縮器(增壓器)機械式耦接,有可能以相同轉速(例如藉助於公共轉軸)或以不同轉速(例如藉助於中間齒輪機制)進行耦接。然而,增壓器原則上亦可藉由使用外部能量,例如藉由使用電動馬達來驅動。在本發明之範疇內,如下文亦將另外詳細解釋,可使用渦輪機增壓器及藉由使用外部能量驅動之增壓器。
在此處使用之語言情形中,液態或氣態流體或亦呈超臨界狀態之流體可在一或多種組分中富含或缺少,其中按莫耳、重量或體積計,「富含」可表示至少75%、90%、95%、99%、99.5%、99.9%或99.99%之含量且「缺少」可表示至多25%、10%、5%、1%、0.1%或0.01%之含量。術語「主要」可對應於剛剛給出之「富含」的定義,但尤其係指超過90%之含量。若在此例如提及「氮氣」,則可考慮純氣體或另外富含氮氣之氣體。
術語「壓力位準」及「溫度位準」在下文中用於表徵壓力及溫度,此等意欲表述,壓力及溫度不必以精確壓力/溫度值之形式使用來實現發明概念。然而,此等壓力及溫度通常在例如平均值周圍的±1%、5%、10%、20%或甚至50%之特定範圍內變化。不同壓力位準及溫度位準有可能在此處於不相交範圍中或重疊範圍中。特定而言,壓力位準例如包括不可避免或預期的壓力損耗,例如由於冷卻效果的壓力損耗。溫度位準亦是如此。本文中已巴為單位所報導之壓力位準為絕對壓力。
本發明之優點 在本發明之範疇內,提供一種低成本且同時有效的高氣壓方法。如開始已解釋,此等高氣壓方法在一些情況下表示習知主空氣壓縮器/增壓空氣壓縮器方法的良好替代方案。本發明此處例如係關於一種方法,藉由該方法,可形成31巴下每小時約37 000標準立方米之經壓縮氣態氧、10巴下每小時20 000標準立方米之氣態氮、每小時3000標準立方米之液態氮及每小時3300標準立方米之液態氧,產生同時氬氣。
原則上,各種高氣壓方法自先前技術已知。此等通常基於廠之液體輸出或基於經內部壓縮產品與液態產品之比率進行歸類及區分。在液體輸出沒有那麼高之情況下,如亦在本發明之範疇內所考慮,例如按順序使用所謂的冷增壓器以藉由將過量冷功率轉換為更高氣壓來增加的方法效率。在相應的冷增壓器中,通常將供應至空氣分離廠之饋入空氣之一部分(其在主熱交換器中冷卻至中間溫度位準且有可能已預先增加壓力)帶至更高壓力位準。具有冷增壓器之空氣分離廠揭示於例如EP 3 101 374 A2中。
原則上,在此將冷增壓器理解為意謂饋入有流體之增壓器,該流體在空氣分離廠之位置處在顯著地低於各別環境溫度的溫度位準下,特定而言顯著地低0℃、-10℃、-20℃、-30℃、-40℃或-50℃或甚至低於該溫度位準溫度。有可能藉由冷增壓器來增加方法效率,此係因為相對減少的液體輸出意謂未自系統「提取」相應的冷量,如在相應的產品呈液態形式時,將為此情況。用於本發明之冷增壓器可經設計為渦輪機增壓器或由外部能量驅動之增壓器。
此外,亦已知空氣分離廠之主熱交換器之kF值(亦即熱轉移係數k及熱交換器表面積F之乘積)可藉由使用冷增壓器增加。此可歸因於在冷增壓器中冷壓縮期間獲得之功率在其自身主熱交換器中幾乎完全耗散的事實。因此,儘管改良了內部壓縮方法或熱交換器中之Q-T概況,所需交換表面積變得更大,此係因為某一溫度範圍中之壓縮氣體之量幾乎兩次冷卻。出於說明之目的,應參考例如已提及之EP 3 101 374 A2之圖1。在此,由於溫度因壓縮而增加,物質流i在壓力在冷增壓器101中在比其後該物質流返回至主熱交換器7之溫度位準更低的溫度位準下增加之前自主熱交換器7移除。根據熱力學觀點,Q-T概況之改良可歸因於此溫度範圍中之冷的及溫熱流體之熱容差的增加。
藉由在不同壓力下使用數個節流閥流改良高氣壓方法之效率同樣為已知的。在此情形中,「節流閥流」為在高於主熱交換器中之高壓管柱之操作壓力的壓力位準下冷卻之饋入空氣數量之部分,在相應的壓力下以氣態至少部分地液化或轉換為超臨界狀態且隨後藉助於膨脹裝置(傳統地膨脹閥(「節流閥」))鬆開,且供應至精餾管柱系統,特定而言高壓管柱。
在例如約10巴下之經加壓氮氣產品可例如由增壓壓縮,特定而言作為在約5.5巴下操作之來自高壓管柱之經加壓氮氣,或藉由內部壓縮提供。在第一情況中,需要分離壓縮器,在後者情況中,需要內部壓縮泵及另外更大的熱交換器。
在本發明之範疇內,在開始解釋的提供低成本且仍然有效的HAP方法的問題因此藉由提供以下來解決:代替如自先前技術原則上已知之用於改良主熱交換器中之Q-T概況的饋入空氣流之冷壓縮,來自高壓管柱之氮氣流在渦輪機增壓器或由外部能量驅動之增壓器中以冷狀態壓縮。此在本發明之範疇內以尤其有利之方式組態及產生。
冷增壓器之壓力比率通常為1.9至2之最大值。在此情況中將壓力比率定義為相應增壓器之輸入壓力與輸出壓力之比率。在本發明之情況中在約10巴下,此壓力比率足以遞送需要數量之氮氣產品。因此,冷增壓器可有利地用於在相應的壓力位準下提供經加壓氮氣。
藉由使用用於相應氮氣產品流之冷增壓器,可達成與藉由在冷增壓器中冷壓縮且隨後冷卻饋入空氣之部分流原則上相同的效果。在此情況中,Q-T概況之改良同樣藉由冷流與溫熱流之間的熱容之更有利比率來達成。然而,與已知方法相比,差異在於,在本發明之範疇內所提出之組態之情況下,冷流之熱容在熱交換器之某些區域中減少(藉由將相應的氮氣流分流至冷增壓器)。在另一方面,在用於先前技術中之空氣之增壓壓縮之情況下,溫熱流之熱容藉由兩次穿過熱交換器之冷壓縮空氣流增加。所描述之差異對熱交換器之kF值具有積極影響。此在本發明之範疇內減少,此係因為用於經加壓氮氣之冷增壓器之功率不一定必須耗散於主熱交換器中(經加壓氮氣流因壓縮而升溫且隨後在適合點處反饋至主熱交換器中以用於隨後升溫至幾乎環境溫度)。
除經加壓氮氣產品之冷壓縮以外,本發明亦包含在整個方法中尤其有利的平衡過量的冷功率及冷增壓器之功率。在本發明之一尤佳實施例中,此可藉由提供以下來達成:除產品數量以外,亦同時壓縮來自高壓管柱之某一額外數量之經加壓氮氣且隨後用作主熱交換器中之額外節流閥流。因此,相應的額外數量之經加壓氮氣至少部分地在主熱交換器中液化且再次饋入至精餾管柱系統,特定而言高壓管柱中。
以此方式,幾乎耗盡冷增壓器之全部功率且熱交換器中之Q-T概況藉由額外節流閥流改良。在某個意義上,此組態表示用於改良Q-T概況之兩種描述方法之組合。使用額外氮氣節流閥流亦對產品產率具有積極效果,此係因為以此方式,較少空氣經預液化(代替饋入空氣,來自高壓管柱之經加壓氮氣經液化)。
如下文再次所提及,精餾之相應調適在此亦具有重要性。為能夠自氬氣產率未降低之壓力管柱移除更多經加壓氮氣,低壓管柱應經氬氣最佳化,亦即經組態在氬氣冷凝器之饋入點之間,在例如使用粗及純氬氣管柱或氬氣排出管柱時具有額外精餾區段。額外氮氣節流閥流之數量在此情況下表示用於最佳化之參數。自高壓管柱移除及既不經冷凝且作為回流再循環至該高壓管柱中亦不經冷凝且用作液體回流至低壓管柱(如在此之情況)中之所有氮氣根本上損害了低壓管柱中之分離,此係因為其在此不再可用作為回流。
總而言之,本發明提出一種用於藉由使用空氣分離廠而獲得一或多種空氣產品的方法,該空氣分離廠具有精餾管柱系統,其包含高壓管柱及低壓管柱,;以及該空氣分離廠亦配備有主熱交換器及主空氣壓縮器。如已提及,本發明與高氣壓方法結合使用,因此在主空氣壓縮器中將供應至精餾管柱系統之總空氣壓縮至第一壓力位準且在第二壓力位準下操作高壓管柱,該第二壓力位準低於第一壓力位準至少3巴。對於另外的典型壓力差異,應明確地參考前言中給出之解釋。
此外,如原則上已知,在本發明之範疇內,氣態富氮流體在第二壓力位準下自高壓管柱移除且在不預先液化之情況下以該氣態形式升溫。在習知空氣分離廠中,此流體為經加壓氮氣,其將作為方法之產品自空氣分離廠移除。通常,此富氮流體在主熱交換器中完全地升溫且隨後作為相應的產品釋放。若在此提及「在不預先液化之情況下」以氣態形式升溫之相應的流體,則此應理解為意謂相應的流體不為自高壓管柱移除,以熱交換方式在連接高壓管柱及低壓管柱之主冷凝器中液化且隨後例如返回至高壓管柱或饋入至低壓管柱中之此氮氣。此流體原則上亦可升溫或例如用於提供液態氮。亦可在本發明之範疇內使用相應的流體(但除在不預先液化之情況下以氣態形式升溫之流體以外)。
在此方面在本發明之範疇內設想將第一部分數量之氣態富氮流體升溫至-150至-100℃,特定而言-140至120℃,例如-130℃之第一溫度位準,在此第一溫度位準下將其供應至增壓器且藉由使用增壓器將其進一步壓縮至第三壓力位準。由於將氣態富氮流體及第一部分數量之此流體供應至增壓器的溫度位準,增壓器在上文解釋之意義上為「冷增壓器」。如已解釋,此增壓器可經設計為渦輪機增壓器或藉助於外部能量驅動之增壓器。上文同樣已提及使用冷增壓器之優點。第三壓力位準特定而言在將相應的氮氣產品釋放之壓力位準下,例如在8至12巴,特定而言9至11巴,例如10巴之壓力下。因此,此壓力位準為其中釋放相應的富氮經加壓產品的壓力。
在本發明之範疇內亦設想在壓縮至第三壓力位準之後將第一部分數量升溫至高於第一溫度位準之第二溫度位準,其特定而言可在環境溫度下,且將其自空氣分離廠永久性排出。因此,相應的第一部分數量作為經加壓產品提供。
根據本發明之一尤其有利實施例,亦設想將第二部分數量之氣態富氮流體與先前已提及之第一部分數量一起同樣升溫至第一溫度位準,在此第一溫度位準下將其供應至增壓器,且藉由使用增壓器將其進一步壓縮至第三壓力位準。然而,在此設想在壓縮至第三壓力位準之後將該部分數量冷卻至低於第一溫度位準之第三溫度位準,隨後使其膨脹至第二壓力位準且使其返回至高壓管柱。在此情況下,在冷卻至第三溫度位準期間,第二部分數量特定而言至少部分地液化或自超臨界狀態轉換為液態。因此,在此情況下,如所提及,在冷增壓器中壓縮之部分數量(特定而言第二部分數量)之經加壓氮氣用作另外的節流閥流。第三溫度位準可為 -180至-165℃,特定而言-177至-167℃,例如-172℃的溫度位準。
此外,在本發明之範疇內,亦有可能將未壓縮至第三壓力位準的第三部分數量之富氮流體升溫至第一溫度位準且將其自空氣分離廠永久性地排出。相應的氮氣可例如以所謂的密封氣體之形成或作為呈較低壓力位準之氮氣產品提供。第一、第二及第三部分數量較佳地一起形成自高壓管柱移除且不經液化的總數量之富氮流體。
在本發明之範疇內,在以下情況下為尤其有利的:藉由使用主熱交換器將第一及第二部分數量升溫至第一溫度位準;及/或藉由使用主熱交換器將第一部分數量升溫至第二溫度位準;及/或藉由使用主熱交換器將第二部分數量冷卻至第三溫度位準。如已解釋,以此方式,可以尤其有利之方式影響主熱交換器之Q-T概況及kF值。
如所提及,在本發明之一個組態中,將用於壓縮冷氮氣流之增壓器(亦即冷增壓器)耦接至膨脹渦輪機,且因此表示渦輪機增壓器。在此在以下情況下為尤其有利的:在耦接至增壓器之膨脹渦輪機中,將供應至精餾管柱系統且藉由使用主空氣壓縮器先前已冷卻至第四溫度位準且隨後饋入至高壓管柱中之空氣之部分膨脹至第二壓力位準。在此情況下,第四溫度位準可在-170至-120℃下,特定而言在-160℃至-130℃下,例如-149℃。
出於驅動冷增壓器目的而供應至膨脹渦輪機中之精餾系統的部分空氣原則上亦可發生膨脹到大約低壓管柱之壓力位準,隨後將此流引入至低壓管柱中。在某些情況下,亦可為可取的是,在第二壓力位準下將另外的氮氣流自高壓管柱移除,在熱交換器中將其升溫至某一溫度位準且出於驅動冷壓縮器目的在膨脹渦輪機中使該氮氣流膨脹。
作為此之替代方案,冷增壓器亦可藉由使用外部能量驅動,亦即不呈儲存於提供於空氣分離廠中之程序流中之能量的形式。特定而言,電動馬達可用於驅動冷增壓器。
在以下情況下為尤其有利的:第二部分數量包含一定部分的氣態富氮流體,特定而言標準化定量部分,例如以每小時標準立方米表述,0至60%,特定而言10至50%,例如15至35%氣態富氮流體之部分,該氣態富氮流體在第二壓力位準下自高壓管柱移除且在不預先液化之情況下以氣態形式升溫。如所提及,以此方式,可幾乎完全地利用相應的廠之能力。
在以下情況下為尤其有利的:在另外的增壓器中將供應至精餾管柱系統之空氣之一部分自第一壓力位準壓縮至20至30巴,特定而言22至27巴,例如25巴之第五壓力位準,藉由使用主熱交換器將其冷卻至第五溫度位準,在機械式耦接至另外的增壓器之膨脹渦輪機中將其膨脹至第二壓力位準,且隨後將其饋入至高壓管柱中。使用所謂的溫熱增壓器之此程序在此情況下可原則上對應於先前技術且支持可在本發明之範疇內獲得之優點。
在此組態之情況下,證明在以下情況下為尤其有利的:在另外的增壓器中將供應至精餾管柱系統之空氣之一部分自第一壓力位準壓縮至第五壓力位準,藉由使用主熱交換器將其冷卻至第六溫度位準(其在例如-165至-115℃,特定而言在-150℃至-130℃下,例如-141℃),將其膨脹至第二壓力位準,且隨後饋入至高壓管柱中。亦以此方式,可進一步加強可在本發明之範疇內獲得之優點。
在以下情況下亦達成特定優點:藉由使用主熱交換器將以液態形式供應至精餾管柱系統之空氣之部分冷卻至第一壓力位準,使其自第一壓力位準膨脹至第二壓力位準,且隨後饋入至高壓管柱中。對於此組態之特定優點,應參考上文給出之解釋。
特定而言,在本發明之範疇內,精餾管柱系統包含至少一個精餾管柱,將相對於高壓管柱之儲槽液體富集氬氣之第一流體自低壓管柱轉移該精餾管柱中,且其中該第一流體耗盡氬氣。在氬氣耗盡之後留下之第一流體之殘餘物在此情況中以第二流體之形式返回至低壓管柱中。在此情況下,本發明可藉由使用已知之粗氬氣管柱及可能的純氬氣管柱來使用,但亦有可能藉由使用所謂的氬氣排出管柱僅排出氬氣,而不獲得氬氣產品。
由此獲得之自低壓管柱中分離之流體排出氬氣的有利效果可歸因於對於經排出氬氣數量在低壓管柱中不再需要氧氣-氬氣分離的事實。低壓管柱中氬氣與氧氣的分離本身原則上為複雜的且需要主冷凝器之相應的「加熱」功率。若氬氣排出且因此氧氣-氬氣分離消除,或若該氧氣-氬氣分離重新定位至例如粗氬氣管柱或氬氣排出管柱中,則相應的氬氣數量不再需要在低壓管柱之氧氣部分中分離,且可減小主冷凝器之加熱功率。因此,在氧氣產率保持相同之情況下,更多經加壓氮氣可自高壓管柱移除,其在本發明之範疇內為尤其需要的。
在習知粗氬氣管柱中,可獲得粗氬氣且在下游純氬氣管柱中進行製備以形成氬氣產品。相比之下,出於上文解釋之目的,氬氣排出管柱主要用於氬氣排出。可原則上將「氬氣排出管柱」理解為意謂用於氬氣-氧氣分離之分離管柱,其不用於獲得純氬產品但用於自高壓管柱及低壓管柱中之待分離空氣排出氬氣。其之互連僅與典型粗氬氣管柱略微不同,但其顯著含有更少理論塔盤,特定言之少於40,特定而言在15與30之間。如同粗氬氣管柱,將氬氣排出管柱之儲槽區域連接至低壓管柱之中間點,且藉由頂部冷凝器冷卻氬氣排出管柱,在該氬氣排出管柱之蒸發側上通常引入來自高壓管柱之經膨脹儲槽液體。氬氣排出管柱通常不具有儲槽蒸發器。
在此在以下情況下為尤其有利的:使用粗氬氣管柱及純氬氣管柱,分別用頂部冷凝器操作,在該頂部冷凝器中部分地蒸發來自高壓管柱之儲槽的富氧液體(其特定而言預先穿過對流子冷凝器)。未蒸發部分在此情況中分別地以液態形式饋入至低壓管柱中。在此來自純氬氣管柱之頂部冷凝器之未蒸發部分的饋入在高於來自粗氬氣管柱之頂部冷凝器之未蒸發部分的饋入5至15個理論分離級有利地進行,且後者再次高於第一流體之移除及第二流體之反饋。以此方式,可達成「氬氣最佳化」之分離,使得有可能自高壓管柱相應地移除更大數量之富氮流體。
本發明亦係關於一種用於獲得一或多種空氣產品之廠,關於其之特徵參考相應的從屬專利申請範圍。
對於根據本發明所提出之空氣分離廠之特徵及優點,應明確地參考上文關於根據本發明所提出之方法所給出之解釋。相同亦相應地適用於空氣分離廠,該空氣分離廠設置用於實行諸如上文詳細解釋之方法且具有相應的用於此之構件。
下文參考附圖更詳細地解釋本發明,其說明本發明之較佳實施例。
在圖1中,根據本發明之一個實施例之空氣分離廠以簡化示意性圖示展示且由100指代。
在空氣分離廠100中,饋入空氣流(AIR)藉助於主空氣壓縮器1經由過濾器2吸入且壓縮至在本文中稱為第一壓力位準的壓力位準。主空氣壓縮器1可特定而言經設計呈具有中間冷卻之多級。分配至主空氣壓縮器1之冷卻器經展示作為數個相應的冷卻器之代表且由3指代。
在空氣分離廠100中實行之空氣分離方法為上文解釋之高氣壓方法,使得第一壓力位準在高於用以操作空氣分離廠100之精餾管柱系統(參見下文)之高壓管柱14的壓力位準至少3巴,且後者壓力位準在本文中稱為第二壓力位準。
饋入至精餾管柱系統的空氣之總數量(其壓縮至第一壓力位準)在本文中稱為饋入空氣數量。此饋入空氣數量首先以饋入空氣流之形式在冷卻裝置4中經冷卻,且隨後在吸收裝置5中釋放至少大部分水及二氧化碳。關於冷卻裝置4及吸收裝置5之操作原理,應參考專業文獻,諸如Häring (參見上文)。冷卻裝置4以冷卻水(H2
O)描述之方式操作;吸收裝置5用再生氣體再生,該再生氣體在使用其之後可釋放至大氣(ATM)。冷卻及純化饋入空氣流a,為允許較佳區分,因此由b指代,首先分為兩個部分流c及d。
在機械式耦接至膨脹渦輪機7之增壓器6中將部分流c帶至高於第一壓力位準之壓力位準,且在冷卻之後,在後冷器中再次分為兩個部分流e及f,其供應至空氣分離廠100之主熱交換器9。由於部分流e在環境溫度下或更高溫度下(但至少高於0℃之溫度位準)供應至增壓器6,其亦稱為溫熱增壓器。部分流e在中間溫度位準下自主熱交換器9移除,在膨脹渦輪機7中膨脹且以至少部分地氣態之形式饋入至高壓管柱14中。部分流f自冷側上之主熱交換器9移除且以液態形式經由節流閥10饋入至高壓管柱14中。部分流f因此為第一節流閥流。
將部分流c同樣再次分為兩個部分流g及h,其供應至空氣分離廠100之主熱交換器9。部分流g在中間溫度位準下自主熱交換器9移除,在機械式耦接至增壓器12之膨脹渦輪機11中膨脹,且以至少部分地氣態之形式饋入至高壓管柱14中。其在此情況中預先與部分流e組合。如下文所解釋,由於將顯著低於環境溫度,但至少顯著低於0℃、-10℃、-20℃、-30℃、-40℃、-50℃之流體供應至增壓器12,所以其亦稱為冷增壓器。部分流h自冷側上之主熱交換器9移除且以液態形式經由節流閥13饋入至高壓管柱14中。其在此情況中預先與部分流f組合或直接地饋入至高壓管柱14中。部分流h因此為第二節流閥流。
操作精餾管柱系統(其在空氣分離廠100中包含已提及之高壓管柱14、低壓管柱15、粗氬氣管柱16及純氬氣管柱17)可原則上獲自開始所引用之專業文獻。
空氣分離廠100經設計以用於內部壓縮。出於此目的,在所呈現之實例中,呈物質流i形式之富氧儲槽產品以液態形式自低壓管柱15移除且在內部壓縮泵18中將呈物質流k形式之其部分帶至大約30巴(a)或更高壓力位準,例如超臨界壓力位準,在主熱交換器9中將其自液態蒸發或轉換為超臨界狀態,且在廠之周邊處作為經內部壓縮之富氧空氣產品(GOX IC)釋放。物質流i之另外部分不經內部壓縮,替代地將其以物質流l之形式傳遞至廠之周邊且在此作為液態氧氣產品(LOX)釋放。在此情況下,溫度可藉由部分地穿過物質流l經由對流子冷卻器19設置。
呈物質流m形式之富氧液體可自高壓管柱14之儲槽移除。物質流m可穿過對流子冷卻器19且隨後部分饋入至粗氬氣管柱16及純氬氣管柱17之頂部冷凝器之各別蒸發空間中。將自此等蒸發空間移除之液態及氣態部分饋入至低壓管柱15中。以已知方式操作粗氬氣管柱16及純氬氣管柱17。特定而言,呈物質流n形式之富氬流體在適合位置處自低壓管柱15移除且在粗氬氣管柱16中耗盡氧氣,其返回至低壓管柱15中。將含氮粗氬氣以物質流o形式轉移至純氬氣管柱中,在該純氬氣管柱中特定而言可分離出氮氣且釋放至大氣(ATM)。液態氬(LAR)可在廠之周邊處作為產品釋放。
氣體可自低壓管柱15之頂部移除且以物質流p之形式穿過對流子冷卻器19,且隨後經由主熱交換器9 (亦參見連接A),且在加熱裝置20中升溫之後在吸收裝置5中可部分地用作已提及之再生氣體。原則上亦有可能將其釋放至大氣(ATM),例如在其中不再需要再生氣體時。液態富氮物質流q可在低壓管柱15之上部區域中自塔盤抽出且在廠之周邊處作為液態產品(LIN)釋放。
液態空氣可以物質流r之形式自高壓管柱14抽取,穿過對流子冷卻器19且饋入至低壓管柱15中。呈物質流s之形式的富氮氣體可自高壓管柱之頂部抽出。此可以物質流t之形式在以熱量交換方式連接高壓管柱14及低壓管柱15之主冷凝器21中部分地經液化,且用作高壓管柱14之回流,且亦穿過對流子冷卻器19並饋入至低壓管柱15中。
所說明之實施例中之本發明之另一態樣為處理不穿過主冷凝器21之物質流s之部分。由於其已自高壓管柱移除,所以其在後者之壓力位準(第二壓力位準)下,且在呈現之實例中以物質流u之形式供應至冷側上之主熱交換器9。部分流v自溫側上之主熱交換器9移除且例如作為密封氣體提供。
另外的部分流w在中間溫度位準下自主熱交換器9移除,該中間溫度位準在本文中稱為第一溫度位準,且在已提及之增壓器12中將其帶至高於第二壓力位準之壓力位準,該壓力位準在本文中稱為第三壓力位準。繼而,將部分流w之部分流x再次供應至主熱交換器9,自冷側上自該主熱交換器移除,亦即冷卻至在本文中稱為第三溫度位準之溫度位準,以液態經由節流閥22膨脹且返回至高壓管柱14之上部區域中。部分流x因此為另外的節流閥流。
在另一方面,在主熱交換器9中使部分流w之另外的部分流y升溫至在本文中稱為第二溫度位準之溫度位準,且在廠之周邊處作為氣態經加壓氮氣產品釋放。
換言之,在此藉由使用主熱交換器9,將呈富氮流體(其在第二壓力位準下以物質流u之形式自高壓管柱15移除,且藉由使用主熱交換器9升溫)之物質流y及x之形式的第一部分數量及第二部分數量升溫至第一溫度位準,在此溫度下水平下供應至增壓器12,且藉由使用增壓器12進一步壓縮至第三壓力位準。在壓縮至第三壓力位準之後,藉由使用主熱交換器9將第一部分數量(亦即物質流y)升溫至高於第一溫度位準之第二溫度位準且自空氣分離廠永久性排出。在壓縮至第三壓力位準之後,藉由使用主熱交換器9將第二部分數量(亦即物質流x)冷卻至第三溫度位準,膨脹至第二壓力位準且返回至高壓管柱15中。
圖2以示意性圖示展示根據本發明之另一實施例之空氣分離廠,未給出關於圖1已解釋之組件的描述。其亦不再次以名稱提供。
如圖2中所說明,類似於根據廠100或圖1之物質流k (參見圖2中之連接X),主冷凝器21中液化之富氮氣體之一部分亦藉助於另外的內部壓縮泵201壓縮,在主熱交換器9中升溫且隨後作為經內部壓縮之氣態氮氣產品(GAN IC)提供。
圖3以示意性圖示展示根據本發明之另一實施例的空氣分離廠。再次,未給出關於圖1或圖2已解釋之組件的描述。其亦不再次以名稱提供。
如圖3中所說明,代替由部分流c形成之部分流g,部分流d之另外部分流301 (因增壓器6中壓縮而係在比部分流c更高的壓力位準下)亦可替代地供應至膨脹渦輪機11。在此情況中不形成部分流g。
圖4以示意性圖示展示根據本發明之另一實施例的空氣分離廠。如前所述,在此亦未給出關於先前圖式已解釋之組件的描述,且在此其不再次以名稱提供。
如圖4中所呈現,增壓器12亦可藉由使用外部能量,例如藉由使用電動馬達M驅動。以此方式,有可能省去單獨提供物質流g (圖1)或301 (圖3)。
1‧‧‧主空氣壓縮器
2‧‧‧過濾器
3‧‧‧冷卻器
4‧‧‧冷卻裝置
5‧‧‧吸收裝置
6‧‧‧增壓器
7‧‧‧主熱交換器/膨脹渦輪機
9‧‧‧主熱交換器
10‧‧‧節流閥
11‧‧‧膨脹渦輪機
12‧‧‧增壓器
13‧‧‧節流閥
14‧‧‧高壓管柱
15‧‧‧低壓管柱
16‧‧‧粗氬氣管柱
17‧‧‧純氬氣管柱
18‧‧‧內部壓縮泵
19‧‧‧對流子冷卻器
20‧‧‧加熱裝置
21‧‧‧主冷凝器
22‧‧‧節流閥
100‧‧‧空氣分離廠
201‧‧‧內部壓縮泵
301‧‧‧部分流
a‧‧‧空氣流
b‧‧‧部分流
c‧‧‧部分流
d‧‧‧部分流
e‧‧‧部分流
f‧‧‧部分流
g‧‧‧部分流/物質流
h‧‧‧部分流
i‧‧‧物質流
k‧‧‧物質流
l‧‧‧物質流
m‧‧‧物質流
n‧‧‧物質流
o‧‧‧物質流
p‧‧‧物質流
q‧‧‧物質流
r‧‧‧物質流
s‧‧‧物質流
t‧‧‧物質流
u‧‧‧物質流
v‧‧‧部分流
w‧‧‧部分流
x‧‧‧部分流/物質流
y‧‧‧部分流/物質流
圖1以一示意性圖示展示根據本發明之一個實施例的空氣分離廠。 圖2以示意性圖示展示根據本發明之一個實施例的空氣分離廠。 圖3以示意性圖示展示根據本發明之一個實施例的空氣分離廠。 圖4以示意性圖示展示根據本發明之一個實施例的空氣分離廠。
Claims (14)
- 一種用於藉由使用空氣分離廠(100)而獲得一或多種空氣產品的方法,該空氣分離廠(100)具有精餾管柱系統(14-17),其包含高壓管柱(14)及低壓管柱(15);以及亦具有主熱交換器(9)及主空氣壓縮器(1),其中 在該主空氣壓縮器(1)中將供應至該精餾管柱系統(14-17)之總空氣壓縮至第一壓力位準,在第二壓力位準下操作該高壓管柱(15),該第二壓力位準低於該第一壓力位準至少3巴,及 在該第二壓力位準下將氣態富氮流體自該高壓管柱(15)移除且在不預先液化之情況下以該氣態形式升溫,其特徵 在於 將第一部分數量之該氣態富氮流體升溫至-150至-100℃,特定而言 -140至-120℃之第一溫度位準,在此第一溫度位準下供應至增壓器(12),且藉由使用該增壓器(12)進一步壓縮至第三壓力位準,及 在壓縮至該第三壓力位準之後,該第一部分數量升溫至高於該第一溫度位準之第二溫度位準且自該空氣分離廠(100)永久性地排出。
- 如請求項1之方法,其中將第二部分數量之該氣態富氮流體與該第一部分數量一起升溫至該第一溫度位準,在此溫度位準下供應至該增壓器(12),且藉由使用該增壓器(12)進一步壓縮至該第三壓力位準,在壓縮至該第三壓力位準之後,將該第二部分數量冷卻至低於該第一溫度位準之第三溫度位準,隨後膨脹至該第二壓力位準且返回至該高壓管柱(15)中。
- 如請求項2之方法,其中將第三部分數量之未壓縮至該第三壓力位準的該富氮流體升溫至該第一溫度位準且自該空氣分離廠(100)永久性地排出。
- 如請求項2或3之方法,其中藉由使用該主熱交換器(9)將該第一及該第二部分量升溫至該第一溫度位準,及/或藉由使用該主熱交換器(9)將該第一部分數量升溫至該第二溫度位準,及/或其中藉由使用該主熱交換器(9)將該第二部分數量冷卻至該第三溫度位準。
- 如前述請求項中任一項之方法,其中該第三壓力位準為8至12巴。
- 如前述請求項中任一項之方法,其中將該增壓器(12)機械式耦接至膨脹渦輪機(11),特定而言在耦接至該增壓器(12)之該膨脹渦輪機(11)中,將供應至該精餾管柱系統(14-17)且藉由使用該主空氣壓縮器(9)預先冷卻至第四溫度位準並隨後饋入至該高壓管柱(14)中之該空氣之部分膨脹至該第二壓力位準。
- 如請求項1至5中任一項之方法,其中該增壓器(12)藉由使用外部能量,特定而言藉助於電動馬達(M)驅動。
- 如請求項2或從屬於請求項2之請求項中之一者之方法,其中該第二部分數量包含10至50%在該第二壓力位準下自該高壓管柱(15)移除且在不預先液化之情況下以該氣態形式升溫的該氣態富氮流體之部分。
- 如前述請求項中任一項之方法,其中在另外的增壓器(6)中將供應至該精餾管柱系統(14-17)之該空氣之部分自該第一壓力位準壓縮至第五壓力位準,藉由使用該主熱交換器(9)冷卻至第五溫度位準,在機械式耦接至該另外的增壓器(6)之膨脹渦輪機(7)中膨脹至該第二壓力位準,且隨後饋入至該高壓管柱(14)中。
- 如請求項9之方法,其中在該另外的增壓器(6)中將供應至該精餾管柱系統(14-17)之該空氣之部分自該第一壓力位準壓縮至該第五壓力位準,藉由使用該主熱交換器(9)冷卻至第六溫度位準,膨脹至該第二壓力位準,且隨後饋入至該高壓管柱(14)中。
- 如前述請求項中任一項之方法,其中供應至該精餾管柱系統(14-17)之該空氣之部分在該第一壓力位準下藉由使用該主熱交換器(9)冷卻,自該第一壓力位準膨脹至該第二壓力位準,且隨後饋入至該高壓管柱(14)中。
- 如前述請求項中任一項之方法,其中該精餾管柱系統(14-17)包含至少一個精餾管柱(16),將相對於該高壓管柱(15)之儲槽液體富集氬氣之第一流體自該低壓管柱(15)轉移至該精餾管柱,且其中該第一流體耗盡氬氣,在氬氣耗盡之後留下之該第一流體之殘餘物返回至該低壓管柱(15)中。
- 如請求項12之方法,其中使用粗氬氣管柱(16)及純氬氣管柱(17),用頂部冷凝器操作,在該頂部冷凝器中,來自該高壓管柱(14)之儲槽的富氧液體部分地蒸發,在高於來自該粗氬氣管柱(16)之該頂部冷凝器之該未蒸發部分的饋入5至15個理論分離級將來自該純氬氣管柱(17)之該頂部冷凝器之未蒸發部分反饋至該低壓管柱(15)。
- 一種用於獲得一或多種空氣產品之廠(100),該廠具有精餾管柱系統(14-17),該精餾管柱系統包含高壓管柱(14)及低壓管柱(15);以及亦具有主熱交換器(9)及主空氣壓縮器,該廠(100)具有經設計用於以下之構件 在該主空氣壓縮器(1)中將供應至該精餾管柱系統(14-17)之總空氣壓縮至第一壓力位準,且在第二壓力位準下操作該高壓管柱(15),該第二壓力位準低於該第一壓力位準至少3巴,及 在該第二壓力位準下將氣態富氮流體自該高壓管柱(15)移除,且在不預先液化之情況下以該氣態形式升溫,其特徵 在於經設計用於以下之構件 將第一部分數量之該氣態富氮流體升溫至-150至-100℃,特定而言 -140至-120℃之第一溫度位準,在此第一溫度位準下將該第一部分數量供應至增壓器(12),且藉由使用該增壓器(12)將該第一部分數量進一步壓縮至第三壓力位準,及 在壓縮至該第三壓力位準之後,將該第一部分數量升溫至高於該第一溫度位準之第二溫度位準,且將該第一部分數量自該空氣分離廠(100)永久性地排出。
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2018
- 2018-05-17 HU HUE18020214A patent/HUE045459T2/hu unknown
- 2018-05-17 EP EP18020214.5A patent/EP3410050B1/de active Active
- 2018-05-17 TR TR2019/10679T patent/TR201910679T4/tr unknown
- 2018-05-17 PL PL18020214T patent/PL3410050T3/pl unknown
- 2018-06-01 US US15/995,742 patent/US11098950B2/en active Active
- 2018-06-01 CN CN201810557870.7A patent/CN109059421B/zh active Active
- 2018-06-01 RU RU2018120350A patent/RU2768445C2/ru active
- 2018-06-01 TW TW107118919A patent/TWI770186B/zh active
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TWI815269B (zh) * | 2021-01-14 | 2023-09-11 | 美商氣體產品及化學品股份公司 | 流體回收製程及設備及系統 |
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US20180347900A1 (en) | 2018-12-06 |
TWI770186B (zh) | 2022-07-11 |
EP3410050A1 (de) | 2018-12-05 |
RU2018120350A (ru) | 2019-12-03 |
RU2018120350A3 (zh) | 2021-11-08 |
PL3410050T3 (pl) | 2019-10-31 |
US11098950B2 (en) | 2021-08-24 |
TR201910679T4 (tr) | 2019-08-21 |
CN109059421B (zh) | 2022-05-31 |
HUE045459T2 (hu) | 2019-12-30 |
RU2768445C2 (ru) | 2022-03-24 |
CN109059421A (zh) | 2018-12-21 |
EP3410050B1 (de) | 2019-05-01 |
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