TW469152B - Method and apparatus for separating air - Google Patents
Method and apparatus for separating air Download PDFInfo
- Publication number
- TW469152B TW469152B TW088100324A TW88100324A TW469152B TW 469152 B TW469152 B TW 469152B TW 088100324 A TW088100324 A TW 088100324A TW 88100324 A TW88100324 A TW 88100324A TW 469152 B TW469152 B TW 469152B
- Authority
- TW
- Taiwan
- Prior art keywords
- stream
- pressure
- nitrogen
- tower
- rectification column
- Prior art date
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Classifications
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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
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
- F25J3/04006—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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
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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
- F25J3/04436—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 at least a triple pressure main column system
- F25J3/04448—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 at least a triple pressure main column system in a double column flowsheet with an intermediate 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
- F25J3/04436—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 at least a triple pressure main column system
- F25J3/04454—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 at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
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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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
- F25J3/04569—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for enhanced or tertiary oil recovery
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
- F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high pressure column of a double pressure main column system
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
- F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/40—One fluid being 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/42—One fluid being nitrogen
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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
69152 A7 B7 五、發明説明(1 ) 本發明乃關於用於分離空氣之方法與裝置。 藉精餾(即分餾)以分離空氣確實係非常熟知的=典型上 ,空氣係飼入由較高壓力精餾塔、較低壓力精餾塔、舆冷 凝器-再沸器所组成之雙精餾塔,其中冷凝通道連通較高 壓力精餾塔之上部區域且再沸通道連通較低壓力精餾塔之 下部區域=氮氣係因此在較高壓力精餾塔中分離且在冷凝 器-再海器中冷凝ϋ所生成冷凝液之一邵份係在較高壓力 塔中作爲回流且冷凝液之其餘部份係使用在較低壓力精餾 塔中。從較高壓力精餾塔之底部取出富含-氧氣之液態空 氣餾份且將其飼入較低壓力精餾塔之中間質量交換區域。 在較低壓力精餾塔之頂部得到氮氣餾份且在其底部得到富 含-氧氣之餾份。因此在較低壓力精餾塔之壓力下得到氮 乳產品3 許多工業程序 '例如油或氣體之提高回收,需要在高壓 下供應之氮氣,其通常較在較高壓力精餾塔操作者爲高。 爲了降低氮氣之壓力由較低壓力精餾塔之壓力提昇至洪應 至製程之氮氣所需之壓力所需要之功,已知者係以氣態之 形式從較高壓力精餾塔取出一些氮氣產物3不過對一給定 之氮氣回收,此較高壓氮氣可以取出之速率係有限的,因 爲従較高壓力精餾塔取出氮氣氣體會降低所生成之液態氮 氣回流量。 本發明之目的係提供一方法與裝置,其能夠操作以消除 前述所提之問題。 根據本發明,其係提供一分離空氣之方法,其中空氣係 -4 - 太叹炫尺度遠,::屮家標4l ί ('\s ) Λ4規格i 公筇) (讀先聞讀背面之注意事項再填寫本S ) 469 15 2 A 7 B7 五、發明説明(2 ) 飼入由較高壓力精餾塔 '較低壓力精餾塔、與第一冷凝器 ,再浠器所组成之雙精餾塔,其中冷凝通道係連通較高壓 力精餾塔之上部區域以冷凝氮氣,而再沸通道係連通較低 壓力精餾塔之下部區域;操作第二冷凝器-再漭器以再沸 在較高壓力精餾塔中得到之液體餾份,且第二冷凝器-再 浠器係藉欲分離之壓縮空氣之第一物流以加熱、該空氣之 第一物流因此被部份或完全冷凝,或藉由操作在較較高壓 力精餾塔中所得者爲高之壓力之另一精餾塔中預分離空氣 之第一物流所生成之富含-氮氣之氣態流以加熱、該富含-氮氣之氣態流因此被部份或完全冷凝:欲分離之壓縮空氣 之第二物流係藉與冷凝氮氣之物流間接熱交換以部份或完 全冷凝,且冷凝氮氣物流之至少一部份係在其與壓縮空氣 之第二物流熱交換之下游處取出以作爲產物. 本發明亦提供一用於分離空氣之裝置,其包括一由較高 壓力精餾塔、較低壓力精餾塔、與第一冷凝器-再沸器所 組成之雙精餾塔,其中冷凝通道係連通較高壓力精餾塔之 上邵區域以在使用時冷凝氮氣,而再濟通道係連通較低壓 力精餾塔之下部區域:第二冷凝器-再漭器,其中再溝通 道係連通較高壓力精餾塔之下部區域,且冷凝通道係直接 連通欲分離之壓縮空氣之第一物流之來源或連通另一精餾 塔之富含-氮氣之氣態流,其係依次連通該來源且在使用 時係操作在較較高壓力精餾塔中所得者爲高之壓力;第一 進一步冷凝器係藉與冷凝氮氣之物流間接熱交換以部份或 完全冷凝欲分離之壓縮空氣之第二物流;以及將泠凝氮氣 -5- ' CNS ) f :;0Χ247Α^ ) (請先閔讀背&之注意事項再填{;本頁 士.-_ 1____ ;_ \. 469152 A 7 --^~~— ____ ^__---- 五、發明説明(3 ) 物流之至少一部份在其與壓縮空氣之第二物流熱交換之下 游處取出以作爲產物之設備。 藉在較高壓力精齒塔之下部區域再讳液體,使提异氣體 上升通過此精餾塔之速率成爲可能,因此在較高磬力精館 塔中提供一有利於氮氣產物從其中取出之區娀;再者藉冷 俠立氣之第二物流,可限制第二冷凝器-再沸器之熱交換 負何,因此在根據本發明之方法與裝置之範例中,有助於 維持與此第二冷凝器_再沸器之操作有關聯之較低熱力學 無效率,其中其係藉壓縮空氣之第一物流以加熱。(通常 當冷凝液係混合物而非純物質時,冷凝與再沸液體間較大 之皿差係需要的。此較高之溫差會造成冷凝器_再漭器之 較無效率操作)。此外,若第二冷凝器-再沸器係藉在造一 步精餾塔中所分離之富含-氮氣之氣態流以加熱,壓縮空 氣之米二物流之冷凝有助於限制進一步精餾塔之尺寸。再 者壓给二氣足弟一物泥之冷凝可使氮氣在比較高壓力精 飽塔之頂邵所得者爲高之壓力下蒸發,藉此降低所需之壓 縮量’其係與型上隨後提昇氮氣產物至特高之壓力、例如 超過100巴所需者。 在根據本發明之方法之範例中,壓縮空氣之第一物流係 飼入第二冷凝器-再沸器中,所生成之部份或完全冷凝之 2氣流較佳係完全飼入較高壓力精餾塔之中間質量交換區 域。在採用進一步精餾塔之範妁中,富含-氧氣之液體物 流較佳係從進一步精餾塔之底部取出且飼入較高壓力精餾 塔以在其中分離。在根據本發明之方法與裝置之所有範例 -6 - 木玖乐尺度辽冗十家揉々() Λ4Α格(:10:χ Ζ9λΛί?·; ' '
(ti先閱讀背面之·;ί意畜.項再填iii本頁)
AT 46 9 15 2 B; 五、發明説明(4 ) 中,部份或完全冷凝之壓縮空氣之第二物流較佳係完全飼 入較高壓力精餾塔之中間區域。在根據本發明之方法與裝 置之所有範例中,具有组成近似空氣之液體物流從較高塵 力精餾塔之中間質量交換區域取出且飼入較低壓力精餾塔 之中間質量交換區域亦是較佳的。此外,部份或完全冷凝 之第一空氣物流之一部份及/或部份或完全冷凝之第二空 氣物流之一部份亦可以飼入較低壓力精餾塔之中間質量交 換區域。壓縮空氣之第一與第二物流在相同之壓力下壓縮 係較佳的。此可使其取自相同之來源、且在提供壓縮空氣 之第一與第二物流時可採用相當簡單之空氣壓縮系統。 該冷凝氮氣流之部份較佳係以高於較高壓力精餾塔之頂 部處之壓力泵送至其與壓縮空氣之第二物流熱交換之上游 處。 典型上,產物氮氣流係以氣態之形式從較低壓力精餾塔 中取出。爲了提昇根據本發明之方法與裝置所能得到之液 氮量,在較低壓力精餾塔中與液體質量交換之氮氣氣體流 較佳係取出且冷凝。爲此目的可使用第二進一步冷凝器。 較佳係從較低壓力精餾塔中取出之富含-氧氣之液體流 係經降壓且採用於冷凝氮氣氣體流=典型上,由較低壓力 精餾塔中取出與液體質量交換之氮氣氣體冷凝所形成之某 些液氮係採用於符合液氮在該塔中所需之回流=不過通常 藉此冷凝會製造過量之液氮。因此某些冷凝液較佳係泵送 至較高壓力精餾塔且可以使用於補充該塔中之回流、或補 充用於與壓縮空氣之第二物流間接熱交換之液氮。不過液 (請先?4讀背面之注意事項再填3本頁 裝 -7- 46 9 I 5 2 Λ7 B7 五、發明説明(5 氮從第二進—步冷凝器泵 於送至輿壓縮空气、〜 、較高壓力猜餾塔之速率係小 請 先 閱 讀 背 面 意: S 再 填 本 頁 根據本發明之二:流熱交換之液氮速率= 物或氬氣產物下採二裝既典型上係在不生產任何純氧產 精餾塔底部之氧〒.八虱义產生。所以因此在較低壓力 範圍内= 耳分率可韓制在G.55至〇.75之値 較佳地是將㈣胃 … 力之欲分離空奢黛二仏、、^ '弟一芏軋物流爲鬲之壓 較低壓力精_中—、/楮對外作功之性能㈣脹且飼入 括-用於將第三空氣=根二本發明之裳置較佳係額外包 者之昇墼-壓_ 必力提昇至高於第一空氣物流 倒以膨=:二^於第三空氣物流藉對外作功 / k ,尚輪機,其具有與該 出口連接之入口以乃由ap u璣之 及與T父低壓力精餾塔之中間質量 域連接之出口,所冶A、π , 貝夏人换£ ^ 斤〜仃乏封外作功較佳係第三空氣物流+ 麼縮’故爲此目的,曰网· 〜 的开壓··塾縮機較佳係採用膨脹渴輪撫 所驅動者。 釉瑪 持別疋在根據本發明之方法與裝置之範例中,其中欲分 離之ΐ7壓縮空氣物流係藉與在較高壓力精餾塔之下部! 域所4到之液體、壓縮空氣之物流及/或從較高壓力精餾 塔工中間質量交換區域所取出之液體問接熱交換以部份或 冗全冷凝,其較诖係在中問壓力精餾塔移除氮氣,該塔係 操作在使其頂部之壓力大於較低壓力精餾塔之底部婴力且 其底部之壓力大於較高壓力精餾塔之頂部壓力。將分離出 4氛氣冷凝且再浠在中間壓力精餾塔下部區域所得到之富 -8 - ( i'NS ^ Λ4:ί!ΰϋ ; :!〇/297^^ 469 15 2 A7 B7 r.i 五、發明説明(6 含-氧氣之液體餾份。所以根據本發明之裝置較佳係額外 包括一具有用於冷凝空氣流及/或從較高壓力精错塔之中 間質量交換區域所取出之液體之入口之中間壓力精館拔, 該中間壓力精飽塔具有一用於冷凝與其之上部區域有關之 氣氣之冷凝器以及與其下部區域有關之再沸器。中間愚力 精餾塔之操作使進一步提昇可用於安***餾塔之回流成爲 可能且藉此使在第一冷凝器_再沸器中冷凝之氮氣之速率 可以取出以作爲產物。 〜 在中間壓力精餾塔之下部區域所得到之含氧氣之液體 餾份較佳係藉取自較高壓力精餾塔之氮氣氣體流以再漭。 Q此與中間壓力精箱塔之下部區域有關之再沸器具有輿來 自較高壓力精餾塔之氮氣氣體之出口有關之冷凝通道= 在^間壓力精餾塔分離出之氮氣較佳係藉與在中間壓力 精餾冷乂下部區域所得到t含_氧氣之液體餾份物流間接 $ X換以冷凝,該含-氧氣之液體餾份物流係在其盥從造 一步之精齒塔所分離出之氮氣熱交換之上游處降I所以 在根據本發明之裝置中,與中間I力精料之上部區域有 冷凝器較佳係具有冷卻通道,其係從上游端經降壓關 上接至用於富含-氧氣之液體從中間壓力精餾塔之下部區 離開之出口。 q根據本發明之方法係特別適用在操作於相當高之壓力。 因泛,倒如較低壓力精餾塔之頂部可以操作在25至5巴之 壓力範团内。 土 ^ 該空氣物流可以取自壓縮空氣之來源,其已藉從其中萃 ί諳先閲讀背Φ之注意事項再填寫本頁 ^-----.. VJ *-° 4 6 9 15 2 第88100324號專利申請案 A7 中文說明書修正頁(89年9月) B1 經濟部中央標準局貝工消费合作社印製 五、發明説明(7 ) 取水汽、二氧化碳、與若有需要、烴類以純化,且其已與 分離空氣之產物間接熱交換以冷卻。 ^ 此處所用之術語「精餾塔」包括任何蒸餾或分餾塔、 區,其中液相與汽相係反向接觸,例如藉汽相與液相在安 裝於塔或區中之填充组件或一系列垂直間隔塔板或塔盤上 之接觸以進行流體混合物之分離。一精餾塔可以由數個在 分離塔槽中之區段所組成,以避免具有過高之單塔高度。 根據本發明之方法與裝置現可以藉參考所附圖示之範例 以說明,其中圖1、2與3全係各分離空氣工廠之流程圖。 該圖示並非比例的,不同圖示之相同部件係以相同之參 考號碼標示。 主要元件代表符號 2 主空氣壓縮機 28 入口 4 吸附單元 30 收集器 6 主熱交換器 32 出口 8 熱端 34 熱交換器 10 冷端 36 節流閥 12 雙精餾塔 38 入口 14 較高壓力精顧塔 40 出口 16 較低壓力精餾塔 42 節流閥 18 第一冷凝器-再沸器 44 入口 20 第二冷凝器-再沸器 46 昇壓-壓縮機 22 定出液汽接觸表面之組件 48 後冷卻器 24 入口 50 膨脹渦輪機 26 進一步冷凝器 52 入口 -10 - ----------裝------訂·------j (請先Μ讀背面之注意事項再填寫本頁) 本纸張尺度適用中國國家標準(CNS ) Α4規格(210X297公釐) 469152 第88100324號專利申請案 A7 中文說明書修正頁(89年9月) B7 經濟部中央標準局員工消費合作钍印製 五、發明説明(7a) 54 液-汽接觸組件 82 節流閥 56 第二進一步冷凝器 90 中間壓力精餾塔 58 收集器 92 再沸器 60 節流閥 94 冷凝器 62 出π 96 節流閥 64 泵 98 液-汽接觸組件 66 泵 100 節流閥 70 進一步精餾塔 102 出π 72 入口 - -104 節流閥 74 進一步熱交換器 106 入口 76 節流閥 108 出口 78 液汽接觸组件 110 節流闕 80 節流閥 參考圖1之圖示,空氣流係在主空氣壓縮機2中壓縮*其 具有與其相關之後冷卻器(未示)五係在吸附單元4中純 化。該純化包掊從空氣流中移除相當高沸點之雜質,特別 是水汽與二氧化碳,否則其將在工廠之低溫部件内結凍。 單元4可以藉壓力擺動吸附或溫度擺動吸附以進行純化。 單元4可以額外地包括一或多個催化劑層以移除一氧化碳 與烴類雜質。此一氧化碳與烴類雜質之移除係描述於EP-A-4 3 8 2 82中。此種吸附純化單元之組態與操作係熟知的且 不需在此進一步描述。 — 在純化單元4之下游處空氣流從其熱端8通過主熱交換器 6至其冷端10。該空氣因此冷卻至適合或只稍高於其藉精 餾以分離之溫度。在主熱交換器6之冷端1 0之下游將冷卻 後之空氣流分成第一與第二壓縮空氣流。第一與第二壓縮 -10a· l·* - I — I. !-1- - - I — . 1 ------- ^—« ___—11__ 、1·、·'1 (請先閲讀背面之注意事項再填寫本頁) 本紙張尺度適用中國國家標準(CNS ) A4規格(210X 297公釐) 6 I---- 4 經濟部中央標準局貞工消費合作社印製 9 15 2 第8810〇324號專利申請案 ^ 个又說明書修正頁(89年9月)五、發明説明(8 ) 空氣流係在由較高壓力精餘塔14、較低壓力㈣塔16、斑 第:冷凝器再滞器18所組成之雙精館塔Η中分.離其'中 ~ =通道(未7F )係連通較高壓力精館塔之上部區域以冷 氮氣’而再;弗通道(未示)則係連通較低壓力精飽塔之S 區域》 4 第一空氣流係通過第二冷凝器_再滞器20之冷凝通道(未 示),其係(如所示)位於較高壓力精餾塔14之底部’但其 亦可以位於塔丨4之外部。較高壓力精料14下部區域中之 底部液體餾份係在第二冷凝器-再沸器2〇之再沸通道(未示) 中再滞。較高壓力精掏塔"含有定出液汽接觸表面之组件 22,以使從第二冷凝器-再沸器2〇上昇之汽體與在第一冷 凝器-再沸器18中冷凝之液氮密切質量交換。結果,氮氣 k上昇之ί飞體中分離出。來自第二冷凝器-再沸器2〇之部 份或芜全冷凝之第一空氣流經由入口 24流進較高壓力精餾 塔14之中間質量交換區域。 壓縮空氣之第二物流係流過進—步泠凝器26之冷凝通 道,其係在其中部份或完全冷凝。所生成之部份或完全冷 凝之第二空氣物流係經由通常與入口 2 4在相同高度之入口 2 8飼入較高壓力精餾塔1 4中。 在較高壓力精餾塔14中由空氣所分離出之氮氣係在第— 冷凝器-再沸器18之冷凝通道(未示)中冷凝,且所生成之 冷凝氮氣係回送至較高壓力精.餾塔Μ中之收集器3〇。液氮 回流係從收集器30分散至塔14中。從較高壓力精餾塔14之 底部經出口 32取出之富含-氧氣之液體物流係藉通過熱 -11 - 本紙張尺度適用中國國家標準(CNS ) A4規格(210X297公釐) — ----- - - - I---If n I! —I (N 1* ___, .! I i·^ i靖先聞讀背面之注意事項再填寫本頁} A7 B7 4 R 9 1 5 2 第88100324號專利申請案 °中文說明t修正頁(S9年9月) 五、發明説明(9 ) 交換器3 4以過冷,且經節流閥3 6與入口 3 8飼入較低壓力精 餾塔1 6中。二個其他之氧氣-氮氣混合物物流係飼入較低 壓力精餾塔1 6中以分離。這些物流之其中之一係含有從較 高壓力精餾塔14經通常與入口 24與28在相同高度之出口 4〇 所取出之氧氣與氮氣液體混合物。經出口 40所取出之液體 物流具有近似於離開純化單元4之空氣之組成。經出口 4〇 所取出之液體混合物物流係藉通過熱交換器3 4以過冷,經 過節流閥42以降壓且經典型上較入口 3 8為高之入口 44詞入 較低壓力精餾塔1 6中。壓縮空氣之第三物流亦飼入較低壓 力精餾塔1 6中。壓縮空氣之第三物流係取自主熱交換器6 之熱端8之上游之純化空氣’且係在异壓一壓縮機μ中進 一步壓縮,其係藉通過後冷卻器4 8以從其中移除壓縮熱, 且係從其熱端8通過主熱交換器6。第三壓縮空氣物流係從 主熱交換器6之中間區域取出且在膨脹渦輪機5 〇中膨脹q 所生成之膨脹空氣物流係從膨脹渦輪機50經與入口 38在相 同高度之入口 52以進入較低壓力精餾塔16中。膨脹滿輪機 5 0係與昇壓-壓縮機4 6連結在一起,使膨脹之空氣可以藉驅 動壓縮機46以作功。 前述所提之物流在較低壓力精餾塔1 6中分離成頂部之氣 氣汽體餾份、其係本質上純化的、典型上含有超過99·9體 積%之氮氣,以及不純之底部富含-氧氣之液態空氣鶴份、 其係不純的、典型上含有55至75體積%之氮氣。以第—冷 凝器-再沸器1 8再沸底部富含-氧氣之液態餾份之一部份, 藉此以提供上昇通過塔】6之汽體流動,且上昇之汽體係 -12- 本紙張尺度仙Ta®家辟(⑽)Α嫩格(2lDX297公瘦1 ~— ---- 裝 — ------訂------A (請先閱讀背面之ii意事項再填转本頁) 經濟部中央樣準局員工消費合作社印裳 4 6 9 15 2 A7 B7 第88100324號專利申請案 中文說明書修正頁(89年9月) 五、發明説明(10) (請先閱讀背面之注意事項再填寫本頁) 與下降之液體藉液-汽接觸組件54接觸以密切地質量交 換’组件54之形式可以為蒸餾板或例如為結構填.充物之填 充物。在較低壓力精館塔1 6頂部所得到之氮氣汽體餾份物 流係在第二進一步冷凝器56中冷凝。所生成之冷凝液係回 送土較低壓力精餾塔1 6中之收集器5 8中’以從其分散至較 低壓力精餾塔16中。第二進—步冷凝器之冷卻係藉使較低 壓力精餾塔16所得到之底部富含-氧氣之液態餾份之一部 份經節流閥60以通蟬其且飼入冷凝器5 6之汽化通道(未示) 以提供。富含-氧氣之液體因此在冷凝器56中冷凝氮氣且 其本身i飞化。所生成之汽體經出口 6 2離開冷凝器5 6,以與 於此處過冷之液體物流反向之方向通過熱交換器34,藉此 才疋供用於熱父換器34之必須冷卻。來自熱交換器34之富 含-氧氣之汽體物流從其冷端丨〇流過主熱交換器6至其熱端 8且排放出工處以作為廢產物。從較低壓力精餾塔丨6之頂 部取出較低壓之汽態氮氣產物且以與富含-氧氣廢物同向之 方向通過熱交換器34與6。 經濟部中央標準局貝工消費合作社印製 在第二進一步冷凝器5 6中冷凝之氮氣典型上係比較低壓 力精飽塔16所需之回流過量。一液氮物流係藉泵64從收集 益· 5 8中取出’該系_係使物流以與氮氣產物流同向之方向通 過熱父換器34至位於較高壓力精餾塔η中之收集器30。一 液氮物流係藉泵6 6從收集器3 〇中取出,其係用以提昇液體 之壓力至高於較高壓力精餾塔中所得之任何壓力。此加壓 之液氮流係藉通過第—進一步冷凝器26以汽化,此係其與 在冷凝器26中部份或完全冷凝之壓縮空氣第二物流間接 -13- 本紙張尺度適用中國圉家標率(CNS) M規格(21〇χ297公) A7 4 69 15 2 五、發明说明(11 ) 熱交換之結果。所生成之汽化加壓氮氣流係從其冷端10通 過主熱交換器6至其熱端8且取出以作爲氮氣產物。S二個 氮氣產物可以在一或多個進一步壓縮機(未示)中進」步整 縮,圖1中所說明之空氣分離方法與裝置之特色爲與傳統 之氮氣產生器相比,其係採用雙精餾塔,負荷係從氮氣產 物壓縮機轉移至主空氣壓縮機2 ^經收集器3 〇從第一冷凝 器-再沸器18中取出液氪產物使較高壓力精餾塔可以相當 有效率地操作,此係因爲少了此液氮產物之取出,特別是 在塔1 4之上邵區域會傾向於過回流。 各種修改與改善可以施加至圖丨之空氣分離工廠中。若 壓縮S氣·^第二物流在冷凝器26中僅部份冷凝,此實施通 常係較冗全冷凝者爲佳,因爲其可降低冷凝器之溫差,所 生成之却访今、喊第二空氣流較佳係送至具有頂部冷凝器( 未π )又相分離器(未示),其之冷凝負荷係藉在分離器中 收集之液相之邵份經閥(未示)之膨脹以提供。液體係從相 分離器中取出且飼入較高壓力精餾塔】4中。此種安排使氮 氣流過冷凝器26之壓力稍微增加,藉此產生氮氣產物壓縮 負荷之對應減低。 將也收集器30取出之氮氣物流通過熱交換器34亦是有利 的。相似地’富含,氧氣之液體物流可以藉通過熱交換器 34以過冷。從較高壓力精餾塔1 4之頂部取出氮汽體物流且 將此物流首先通過熱交換器34且其次從其冷端1 〇通過主熱 交換器ό至其熱端8以在高壓下提供氮氣產物之另一物流亦 是可能的。 _____— -14- 木紙仏尺政邮屮狀笨㈣(( 2ΙΟχ:7ίΓ^Γ) I Tt - Hu __ _ · - flu^ —^m ι·-···、 -- I ^ J. (讀先閱讀背面之注意事項再填¢-7本頁) 6 9 15 2 A7 五·、發明説明(12 ) 在圖I之圖形中张—、 , W工厫(典型操作範例中,較高壓 力精餾塔頂部之厭士 ^ 力係7 ·8巴,較低签力精餾塔16頂部之 壓力係4巴,高壓氧备
鼠乳產物係在丨2巴之壓力下製造且廢氣 純度爲62%。總|[气A 乳乳屋物之4心5%保在較高壓力下製造5 通常,藉增加庳笥朴& ^ ' , 嘥礼‘毛度至7〇%以增加氮氣之取得可以達 成性骷之改吾。此—每、t t 峰 墨力3结 貫-典型上需要增加塔!4與16之搡作 + A*飞產物<壓力增加且因此在氮氣壓縮上所 爸之功降低。此§1认' 、卜 < 功通常超過補償主空氣壓缩機2所 消耗 < 任何増加功。 現參照所附之圖2,娇_, ·产、 M2,所不之空氣分離工廠通常與 者之组態與操作相似、 _ . 產別处瑪弟一冷灰态-再漭器20係 藉在進一步精餘塔7〇 φ时八甘,rp — 一, 中所分離乙'^含-氬氣之汽體物流以 加熱ϋ氣物流係經入口 72以飼入塔70中,且位於主 熱乂換器6與熱X換器34間之進—步熱交換器74係使取自 較低.签力精淘塔1 6之氮氣產物去過冷進-步精餘塔7 0之產 物3因爲壓縮空氣之第-物流係飼入進-步精餾塔70中: 對一給定之玉2氣壓缩機2之出口壓力,較高壓力精餾塔 14係操作在比圖1中所示之工廠較低之壓力。所以,節流 閥76係位於較高壓力精餾塔14之入口 28與冷凝器%間。 Λ (請先聞讀背面之注意事項再填艿本頁 進一步精餾塔70典型上係相當地小且只含有少量 '例如 5個理論板,亦即其含有足夠之液汽接觸组件78以提供5 個理論之分耱暗段,通常,在進一步精餾塔7〇之頂部並不 會得到純氮氣汽體餾份,此餾份典型上含有至少1 〇體積% 之氧氣=富含-氬氣之汽體係在第二冷凝器_再沸器20中冷 -15- 才又度迖圮 彳:rNS > Λ4Α格:2i〇x Δ^9 五、發明説明(13) -- - % - iar mf LJ I (請先㈤請背而之注意事項再填{11本百〇 凝’所生成之泠凝液之—部份係使用在進—步精餾塔7〇以 作爲回流。藉通過熱交換器74以遇冷之其他部份係通過節 流閥8 0且在接近液汽接觸設備2 2之頂部之高度處飼入較高 壓^精錯塔丨4中。從進一步精齒塔7〇之底部取出之富含_ 氧氣之液體物流係藉通過熱交換器74以過冷,通過節流閥 82且在低於入口 28之高度處飼入較高壓力精餾塔14中。 雖..、,在圖2所TF之工摄中’冷凝器_再沸器通常可以較 圖〗所不者馬低(溫差操作,這些溫差可以藉增加進一步 精飽塔70 &頂部處之富含-氮氣之汽禮純度以進一步降低 爲了達到此’可以增加塔7〇之入口壓力、藉此需要更多 功=壓1¾空氣,及/或氮氣回收率可以降低。 圖^與。中听之空氣分離工廠之特色爲較低壓力精餾塔 ^丹沸益1 8芏入口 3 8之區域傾向於相當低效率之操作 .” 了以.藉.會竣麥凱布-帝爾圖以說明^此一圖形將顯示 =作線與平衡線間有明顯之收m中間壓力精館塔中 刀離取自較向壓力精餾塔之下部區域之液體物流可以得到 ?吾之效率,此一裝置係示於圖3中。 二/ 口 3,其顧示一通常與圖1所示者相似之空氣分離工 '&々處爲其包括一具有與其之下部區域有關之再漭器 92和與並夕 p^ 。a ” 部區域有關之冷凝器94之中間壓力精餾塔90 圖洪各種頭外之導管與閥以將中間壓力精餾塔卯整合至 2 λ 之‘〜製中°雖然在圖1所示之工廠中,從較高壓: 六^ j给1 4經出口 4〇所取出之氧氣液體混合物物流係經熱 ’矣器34以冱至較低壓力精餾塔1 6中’此物流係被採用以 、屮 4¾ 家嘌淬 U'NS ) Λ4.ί?^ ( :;0V 297^¥ 4 69 15 2 A7 i___ B7 — '— ---------— ---------—- ____ 五、發明説明(14 ) 一^' ^ 甸入圖3所示之工廠中之中間壓力精餾塔9〇中。所以餘物 流經節流閥96從熱交換器34以流至中間壓力精餾塔^中 3再沸器92係用以蒸發在塔90之底部所收集之液體,所 成之汽體上昇通過塔90且與下降之液體在液-汽接觸組件 %上進行密切之質量交換’组件98可以藉蒸餾板或藉例如 爲結構填充物之填充物以提供。結果,氮氣從流入之液體 中分離出。在塔之頂部所收集之氮氣汽體係在位於塔9〇 $ 頂部之冷凝器94中冷凝。所生成冷凝氮氣之一部份係再飼 入中間壓力精傲塔90之頂邵以提供作爲塔9〇之回流a剩餘 <冷凝氮氣係經節流閥1 0◦流至較低壓力精餾塔〗6中; ° 丁 \岐 集益5 8 〇 氮氣係在冷凝器94中藉與從中間壓力精餾塔9〇之底部經 出口 1 02所取出之富含-氧氣之液體物流間接熱交換以冷赛 1此冨含-氧氣之液體物流係通過節流閥1 〇4以降低其位於 出口〗02與冷凝器94間之溫度=生成之汽體流過出口 ι〇4 J·奴典型上 '但並非必須與入口 5 2在同一高度之入口 1 〇 6 以飼入較低壓力精餾塔1 6中。殘留之液體係經出口丨〇8從 冷凝器94中取出且在通常與入口丨06同一高度處飼入較低 U 壓力精餾塔16中,且於途中通過節流間1 1 〇。 1' 在中間壓力精餾塔90底部之液體係在再海器92中籍與從 ^ 較高壓力精餾塔丨4之頂部所取出之氮氣汽體物流間接熱交 ! 设以再滞。熱交換之結果使氮氣在再沸器92中冷凝,所生 ί1' 成之冷凝液係送回較高整力精鶴塔I 4中之收集器3 〇。 藉將中間壓力精餾塔9 〇整合進空氣分離工處,使可以在 !*:»
V ___ 一 - 17- >1/14 frNS :iOX29-^SS 5 ~~~ f請先閱讀背面之注意事項再填巧本Ij ¾. 、·ρ 9 1 5 2 五、 A7 B7 f明説明( 15 ^譽力下製造〈總氮氣產物之比例增加成爲可能。 在圖J所7F之工廠之—改變中,中間壓力精餾塔9〇之進 L可以部份或完全取自較高壓力精餾塔14之底部。在此一 I例中,在中間壓力精餾塔9〇中所分離之氮氣之純度典型 上係降低,且冷凝之不純氮氣並不需要在塔9〇中作爲回流 ’其係提供至較低壓力精餾塔1 6之中間質量交換區域3 典型上’在圖3所示之工廠之操作中,在中間壓力精餾 塔90頂部處之壓力係6巴3 --------t— (請先聞讀背面之注意事項再填艿本页) ϋ:):·:?-AJniI'·消f^-ϋ.!.>. V. -18
Claims (1)
- 4 9 152第88100324號專利申請案 中文申請專利範圍修正本(89年9月、 六、申請專利範圍 1‘ 一種分離空氣之方法,其中而夯技扣、, 二乳係飼入由較高壓力精餾 - I tt^i ^^^1 -- - - ·111 I— —in .^1^1 ^^^1 一 1 (請先閲讀背面之注意事項再填寫本頁) 塔、較低壓力精銷塔'與第—冷凝器_再滞器所組成之 雙精館塔,其中冷凝通料連通較高壓力精料之上部 區域以冷凝氮氣’而再料道係連通較㈣力精顧塔之 下部區域;操作第二冷凝器-再沸器以再滞在較高壓力 精餾塔中得到之液體餾份,且第二冷凝器_再沸器係藉 欲分離之壓縮空氣之第一物流以加熱、該空氣之第一物 流因此被部份或完.全冷凝,或藉由操作在較較高壓力精 飽塔中所得者為高之壓力之另—精餾塔中預分離空氣之 第一物流所生成之富含-氮氣之氣態流以加熱、該富含_ 氮乳之氣態流因此被部份或完全冷凝;欲分離之壓縮空 氣之第二物流係藉與冷凝氮氣之物流間接熱交換以部份 或完全冷凝,且冷凝氮氣物流之至少一部份係在其與壓 縮空氣之第二物流熱交換之下游處取出以作為產物。 2 .根據申請專利範圍第1項之方法,其中該從較高壓力精 餾塔所取出之冷凝氮氣流之部份係以高於較高壓力精餾 塔之頂部處之壓力泵送至其與壓縮空氣之第二物流熱交 換之上游處。 經濟部中央標準局舅工消費合作社印製 3 ·根據申請專利範圍第1與2項之方法,其中從較低壓力 精餾塔取出之富含-氧氣之液體物流係經降壓且採用於 冷凝從較低壓力精餾塔中取出與液體有質量交換關係之 氮氣汽體物流,且其中產物氮氣物流係以汽態之形式從 較低壓力精销塔中取出。 4 .根據申請專利範圍第3項之方法,其中從較低壓力精餾 塔取出之某些氮氣汽體係在其冷凝之下游處泵送至較高 表紙張尺度逍用中國國家標準(CNS > A4规格(210 X 297公羞) 4 69 15 2 4 69 15 2 A8 B8 C8 D8 ^ A I— 申請專利範圍 壓力精餾塔。 5’二據申請專利範圍第1項之方法,其中壓縮至較第一空 H為壓力 <欲分離之第三空氣物流係對外作功 疋性能以膨脹,且飼入較低壓力精餾塔中β 6 -根據申請專利筋圚筮,g、、,, _ · 弗員又万法,其中冷凝空氣流及/或 從較高壓力精麵塔之中間質量交換區域所取出之液體物 :係在中間壓力精餾塔中從其中分離出氮氣,其係操作 使,、頂部之壓力大於較低壓力精餾塔之底部壓力且並 展部之壓力大於較高壓力精料之頂部壓力,冷凝所^ 離之氮氣且再彿在φ pE)廊+ ^ 即在干間壓力精餾塔之下部區域得到之 含-氧氣之液體餾份。 7·根據申請專利範圍第1項之方法,其中在中間壓力精餘 ,所分離^|L氣係藉與中間壓力精餘塔之該下部區域所 。氧氧之液體餾份物流間接熱交換以冷凝,該 °.'氧氣>之液體餾份物流係在其與中間壓力精餾塔所分 離之氮氣熱交換之上游處降壓,且其中在中間壓力精顧 :、下部區域所得到之含_氧氣之液體餘份係藉從較高 壓力精餾塔取出之氮氣汽體以再沸。 8. —種分離空氣之劈w,甘, t 〇 孔裝置其包括一由較高壓力精餾塔、較 低壓力精餾塔 '與第一冷凝器·再沸器所組成之雙精餾 塔’其中冷凝通道係連通較高壓力精齒塔之上部區域以 在使用時冷凝氮氣,而再彿通道係連通較低壓力精餾塔 4下邵區域;第二冷凝器·再沸器,其中再彿通道係缚 通較高壓力_塔之下部區域’且冷凝通道係直接連通 刀離之壓,揭工氣之第一物流之來源或連通另一精餘塔 X-----—ΐτ (靖先閑讀背面之注意事項再填寫本頁) 經濟部_央標準局貝工消費合作社印裂 張尺度朝悄财 C8 D8 ^ >S- 、申請專利範圍 (请先閲讀背而之注意事項再填寫本頁) 之畐含_亂氣之乳態流’其係依次連通該來源;第一進 一步冷凝器係藉與冷凝氮氣之物流間接熱交換以部份或 完全冷凝欲分離之壓縮空氣之第二物流;以及將冷凝氣 氣物流之至少一部份在其與壓縮空氣之第二物流熱交換 之下游處取出以作為產物之設備。 9.根據申请專利範圍第8項之裝置,在其與壓縮空氣之第 一物流熱交換之上游處額外地包括一用於將冷凝氮氣物 流加壓至鬲於較高.壓力精飽塔之頂部操作壓力之壓力之 泵。 10.根據申清專利範圍第8項之裝置,額外地包括第二進一 步冷凝器’其係與較低壓力精餾塔有關且係配置以冷凝 氮氣。 ί 1.根據申清專利Ιϋ圍弟8項之裝置,額外地包括一用於將 欲分離之第三空氣物流之壓力提昇至高於第一壓縮空氣 物流者之昇壓-壓縮機、以及一用於第三空氣物流藉對 外作功之性能以膨脹之膨脹渦輪機,其具有與該昇壓_ 壓縮機之出口連接之入口以及與較低壓力精鶴塔之中間 質量交換區域連接之出口。 經濟部中央標準局貝工消費合作社印製 12. 根據申清專利範圍第8項之裝置,額外地包括一中間壓 力精餾塔,其具有一用於冷凝空氣流及/或從較高壓力 精餾塔之中間質量交換區域所取出之液體之入口,該中 間壓力精餾塔具有用於冷凝與其之上部區域有關之氮氣 之冷凝器以及與其之下部區斌有關之再沸器。 13. 根據申請專利範圍第π項之裝置,其中與中間壓力精 餾塔之上部區域有關之冷凝器具有從其上游端經壓降 -3- 本紙張从逍财關家縣(CNS )戌4體(21GX297公釐) 4 b9 1 52A、申請專利範国 A8 B8 C8 D8 連接至用於從中間壓力精餾塔之下部區域取出富含-一 氣之液體之出口之冷卻通道,且其中與中間壓力精1 餘= 之下部區域有關之再;'弗器具有連接用於從較高麼力精飽 塔取出氮氣之出口之冷凝通道。 In ^1 HI [ I ^^1 I nJ^^^1 ^^1 ^^1 In (請先E讀背面之注意事項再填寫本f) 經濟部中央標準局員工消費合作社印策 本紙张尺度適用中國國家標準(CNS ) A4規格(2丨0X297公釐)
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GBGB9726954.2A GB9726954D0 (en) | 1997-12-19 | 1997-12-19 | Air separation |
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EP (1) | EP0924486A3 (zh) |
GB (1) | GB9726954D0 (zh) |
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FR2806755B1 (fr) * | 2000-03-21 | 2002-09-27 | Air Liquide | Procede et installation de generation d'energie utilisant un appareil de separation d'air |
DE10018200A1 (de) * | 2000-04-12 | 2001-10-18 | Linde Gas Ag | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff durch Tieftemperaturzerlegung von Luft |
FR2814229B1 (fr) * | 2000-09-19 | 2002-10-25 | Air Liquide | Procede et installation de separation d'air par distillation cryogenique |
CA2347462E (en) * | 2001-05-15 | 2012-03-13 | Kevin Melvin Kjelland | Method and apparatus for reclaiming deicer from produced water of an oil well |
US6397631B1 (en) | 2001-06-12 | 2002-06-04 | Air Products And Chemicals, Inc. | Air separation process |
US9726427B1 (en) * | 2010-05-19 | 2017-08-08 | Cosmodyne, LLC | Liquid nitrogen production |
DE102010056560A1 (de) * | 2010-08-13 | 2012-02-16 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von Drucksauerstoff und Druckstickstoff durch Tieftemperaturzerlegung von Luft |
DE102010056569A1 (de) | 2010-12-30 | 2012-07-05 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff durch Tieftemperaturzerlegung von Luft |
US20130000351A1 (en) * | 2011-06-28 | 2013-01-03 | Air Liquide Process & Construction, Inc. | Production Of High-Pressure Gaseous Nitrogen |
US9097459B2 (en) | 2011-08-17 | 2015-08-04 | Air Liquide Process & Construction, Inc. | Production of high-pressure gaseous nitrogen |
EP2662654A1 (en) * | 2012-05-07 | 2013-11-13 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for the separation of air by cryogenic distillation |
US20160161181A1 (en) * | 2013-08-02 | 2016-06-09 | Linde Aktiengesellschaft | Method and device for producing compressed nitrogen |
JP6557763B1 (ja) * | 2018-08-09 | 2019-08-07 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | 空気分離装置 |
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DE1854836U (de) * | 1958-05-20 | 1962-07-12 | Union Carbide Corp | Vorrichtung zur zerlegung von luft bei niedriger temperatur. |
US4604117A (en) * | 1984-11-15 | 1986-08-05 | Union Carbide Corporation | Hybrid nitrogen generator with auxiliary column drive |
US4594085A (en) * | 1984-11-15 | 1986-06-10 | Union Carbide Corporation | Hybrid nitrogen generator with auxiliary reboiler drive |
US4854954A (en) * | 1988-05-17 | 1989-08-08 | Erickson Donald C | Rectifier liquid generated intermediate reflux for subambient cascades |
CN1027802C (zh) * | 1990-01-19 | 1995-03-08 | 波克集团股份有限公司 | 一种从原料气流中去除杂质的方法 |
US5074898A (en) * | 1990-04-03 | 1991-12-24 | Union Carbide Industrial Gases Technology Corporation | Cryogenic air separation method for the production of oxygen and medium pressure nitrogen |
JP2983393B2 (ja) * | 1991-10-15 | 1999-11-29 | レール・リキード・ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | 高純度窒素の製造における極低温蒸留により水素を除去する方法 |
US5379598A (en) * | 1993-08-23 | 1995-01-10 | The Boc Group, Inc. | Cryogenic rectification process and apparatus for vaporizing a pumped liquid product |
US5355682A (en) * | 1993-09-15 | 1994-10-18 | Air Products And Chemicals, Inc. | Cryogenic air separation process producing elevated pressure nitrogen by pumped liquid nitrogen |
US5402647A (en) * | 1994-03-25 | 1995-04-04 | Praxair Technology, Inc. | Cryogenic rectification system for producing elevated pressure nitrogen |
US5511380A (en) * | 1994-09-12 | 1996-04-30 | Liquid Air Engineering Corporation | High purity nitrogen production and installation |
US5666823A (en) * | 1996-01-31 | 1997-09-16 | Air Products And Chemicals, Inc. | High pressure combustion turbine and air separation system integration |
US5682762A (en) * | 1996-10-01 | 1997-11-04 | Air Products And Chemicals, Inc. | Process to produce high pressure nitrogen using a high pressure column and one or more lower pressure columns |
-
1997
- 1997-12-19 GB GBGB9726954.2A patent/GB9726954D0/en not_active Ceased
-
1998
- 1998-11-30 EP EP98309807A patent/EP0924486A3/en not_active Withdrawn
- 1998-12-17 US US09/215,592 patent/US6141989A/en not_active Expired - Fee Related
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1999
- 1999-01-11 TW TW088100324A patent/TW469152B/zh not_active IP Right Cessation
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GB9726954D0 (en) | 1998-02-18 |
EP0924486A2 (en) | 1999-06-23 |
US6141989A (en) | 2000-11-07 |
EP0924486A3 (en) | 1999-09-29 |
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