TWI737770B - 藉由低溫分離空氣製造加壓氮及液態氮之方法及裝置 - Google Patents

藉由低溫分離空氣製造加壓氮及液態氮之方法及裝置 Download PDF

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TWI737770B
TWI737770B TW106123199A TW106123199A TWI737770B TW I737770 B TWI737770 B TW I737770B TW 106123199 A TW106123199 A TW 106123199A TW 106123199 A TW106123199 A TW 106123199A TW I737770 B TWI737770 B TW I737770B
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nitrogen
stream
low
pressure
pressurized nitrogen
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TW106123199A
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TW201809563A (zh
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帝米特 哥勒貝芙
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德商林德股份公司
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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
    • 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
    • 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
    • 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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    • F25J3/0403—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 nitrogen
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    • 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
    • F25J3/0423—Subcooling of liquid process streams
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    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
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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
    • F25J3/04248—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
    • F25J3/04309—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 nitrogen
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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
    • F25J3/04248—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
    • F25J3/04321—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 oxygen
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    • F25J3/04357—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 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
    • 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
    • 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
    • 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
    • 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
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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
    • F25J2200/94—Details relating to the withdrawal point
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
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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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
    • 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
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • 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
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

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Abstract

本發明揭示一種用於藉由低溫分離蒸餾塔系統中之空氣來製造加壓氮及液態氮之方法及裝置，該蒸餾塔系統具有高壓塔(9)及低壓塔(10)及兩者經設計成冷凝器-蒸發器之主冷凝器(11)及低壓塔頂部冷凝器(12)。空氣(AIR)於主空氣壓縮器(2)中壓縮，被純化(6)，在主熱交換器(8)中被冷卻且經由管線(8')引入至該高壓塔(9)中。來自該低壓塔(10)之該氣態頂部氮之第一部分(44)被排出作為第一加壓氮產品(18，19，PGAN)。來自該高壓塔(9)之頂部之第二加壓氮流(17)在第二膨脹機器(41)中依功執行方式膨脹，且接著被排出作為第二加壓氮產品(43，19，PGAN)。該低壓塔頂部冷凝器(12)中冷凝之該氮(46)之部分(47)被排出作為液態氮產品(PLIN)。

Description

藉由低溫分離空氣製造加壓氮及液態氮之方法及裝置
本發明係關於一種根據專利技術方案1之前言之用於藉由低溫分離空氣來製造加壓氮及液態氮之方法。
已知藉由在空氣分離設備中低溫分離空氣來製造處於液態或氣態之空氣產品。此等空氣分離設備具有可(例如)採用兩塔系統(明確而言，習知林德(Linde)兩塔系統，但亦可採用三塔或多塔系統)之形式之蒸餾塔系統。亦可提供用於獲得其他空氣組分(明確而言，稀有氣體氪、氙及/或氬(參照(例如)F.G.Kerry之Industrial Gas Handbook：Gas separation and Purification，Boca Raton：CRC Press,2006；章節3：Air Separation Technology))之裝置。可將本發明之蒸餾塔系統設計成習知兩塔系統，但亦可設計成三塔或多塔系統。除用於氮氧分離之塔之外，其亦可具有用於獲得其他空氣組分(例如用於獲得不純的、純的或高純度氧氣或稀有氣體)之其他裝置。
「主熱交換器」用於冷卻與來自蒸餾塔系統之再循環流間接熱交換之供給空氣。其可由單一或複數個可操作地連接、並聯及/或串聯連接之 熱交換器區段(例如一或多個板熱交換器區塊)形成。
措詞「冷凝器-蒸發器」係指其中第一、冷凝流體流與第二、蒸發流體流間接熱交換之熱交換器。各冷凝器-蒸發器具有冷凝空間及蒸發空間，其等分別由冷凝通道及蒸發通道組成。第一流體流之冷凝(液化)發生於冷凝空間中且第二流體流之蒸發發生於蒸發空間中。蒸發及冷凝空間由處於熱交換相互關係之通道之群組形成。可將冷凝器-蒸發器之蒸發空間設計成浴槽蒸發器、降膜蒸發器或強制流動蒸發器。
「膨脹機器」可具有任何建構。此處，較佳地使用渦輪機(渦輪膨脹器)。
習知兩塔方法僅具有單一冷凝器-蒸發器、主冷凝器且在相對較低壓力(即，僅高於低壓塔之頂部處之大氣壓)操作。若將獲得大量加壓氮，則使用修改之兩塔方法(其在較高壓力操作)。此使使用低壓塔頂部冷凝器且使用來自蒸餾塔系統之富氧殘餘餾分來冷卻冷凝器變成可行。自US 4453957知道此方法。
迄今，此種類之方法未經考量用於大量液體製造5莫耳%以上之氮產品量。
本發明係基於指示引言中所提及之類型之方法及對應裝置之目標，該方法及該裝置適用於6至10莫耳%之氮產品量或更多之相對較高液體製造，其中在該方法中具有約60%之相對較高氮產品產率，且再者，其有效運作。(氮產率取決於其他參數，例如產品純度。)
此目標係藉由如專利技術方案1之全部特徵來實現。
1:過濾器
2:主空氣壓縮器
3:後冷器
4:冷卻器
5:供給空氣
6:純化器件
7:管線
7A:空氣
7B:空氣
8:主熱交換器
9:高壓塔
10:低壓塔
11:主冷凝器
12:低壓塔頂部冷凝器
13:液態粗氧
14:逆流過冷器
15:管線
16:氣態頂部氮
17:第二加壓氮流
18:第一加壓氮產品
19:第一加壓氮產品/第二加壓氮產品
19A:加壓氮產品
19B:加壓氮產品
20:第二部分
21:液態氮
22:餘料
23:餘料
24:液態富氧餾分
25:管線
26:殘餘氣體流
27:殘餘氣體流
28:第一膨脹機器
29:殘餘氣體流
30:溫熱殘餘氣體
31:管線
32:管線
33:再生氣體加熱器
34:管線
40:第二加壓氮流
41:第二膨脹機器
42:第二加壓氮流
43:第二加壓氮產品
44:第一部分
45:第二部分
46:氮
47:液態氮
50:部分
70:壓縮器級
71:後冷器
72:壓縮器級
73:後冷器
414:逆流過冷器
415:蒸發氮流
416:蒸發氮流/氮
417:閥
550:純氧塔
551:管線
552:管線
553:集液槽蒸發器
554:管線
555:節流閥
556:氣態氮
557:液態氮
558:氣態氧
660:輔助塔
661:高壓塔沖洗液體
662:管線
663:阻擋板
664:集液槽蒸發器
665:空氣部分流
666:空氣
667:頂部氣體
762:管線
763:管線
819:管線/加壓氮產品
820:產品壓縮器
821:產品壓縮器
830:部分
870:液態氮槽
871:液態氮
872:泵浦
873:環境大氣蒸發器
874:加壓氮產品
875a:管線
875b:管線
875c:管線
下文參考圖式中示意性地表示之例示性實施例來更詳細解釋本發明及本發明之進一步細節，其中：圖1展示具有發電機渦輪機之第一例示性實施例，圖2展示具有串聯連接且壓縮空氣之渦輪機加力器之第二例示性實施例，圖3展示具有串聯連接且壓縮氮之渦輪機加力器之第三例示性實施例，圖4展示具有液態氮產品之過冷卻之圖1之第一變體，圖5展示具有純氧之獲得之圖1之第二變體，圖6展示具有用於沖洗來自高壓塔之液體之輔助塔之圖1之第三變體，圖7展示圖6之系統之修改方案，及圖8展示具有液態氮之臨時外部蒸發之系統。
在此內文中，第二加壓氮流自高壓塔之頂部排出且在第二膨脹機器中膨脹至仍允許此流排出作為加壓產品之壓力，較佳地膨脹至約來自低壓塔之頂部之第一加壓氮流之壓力。此外，將低壓塔頂部冷凝器中冷凝之氮之部分排出作為液態氮產品。
此藉由最小外力來使得較大液體製造所需之低溫成為可行。第二渦輪機(其與第一渦輪機相比具有不同入口溫度)亦改良主熱交換器中之溫度分佈(由於較小溫度差而具有較低熱動力損耗)。
在本發明中，較佳地在相同壓力(即，低壓塔之壓力)獲得90莫耳%以上之氣態氮產品。
除約8巴之大量加壓氮之外，吾人熟知需要相對大量之液體產品(LIN)之應用。此等應用包含(例如)半導體工業中之石油化學錯合物或給用戶之現場供應氣體之加油站。在此內文中，液體產品用於滿足需求尖峰(此等可為相當大的，尤其在石油化學設備之情況中)及/或服務外部液體市場。(以上壓力指示(及全部隨後壓力指示，除非另有說明)應理解為絕對壓力)。
迄今，例如藉由結合外部斷續性操作冷凝器使用「光譜」方法(參閱(例如)US 4966002或US 5582034)來實現此等目標。替代地，僅使用光譜設備，其中以大幅減少氣體供應為代價暫時地完成液體製造。第一情況實際上需要兩個設備，其暗指特別高的投資成本。在第二情況中，儘管僅使用一設備，但此具有用於液體製造之十分有限容量；尤其在8巴實施例的情況中，液體製造不僅受限，且亦歸因於渦輪機中之相對較小壓力梯度而低效；一般無法提供液體之所要供應。此外，與本發明中所使用之兩塔方法相比，光譜程序之效率相對較低。
若在8.0巴至9.0巴(明確而言，8.4巴至9.0巴)之壓力自低壓塔之頂部排出第一加壓氮流，則尤其適宜實行根據本發明之方法。
較佳地，第二加壓氮流在膨脹機器中膨脹至約為第一加壓氮流之壓力；接著兩個加壓氮流被結合且排出作為共同加壓氮產品流。最簡單選擇係使此統一發生於主熱交換器中，儘管原則上亦可發生於溫暖環境中，即，主熱交換器之下游。
較佳地，膨脹機器之兩個入口溫度係不同的，明確而言，第二中間溫度高於第一中間溫度至少10K。例如，溫度差介於90K與30K之間，較佳地介於70K與50K之間。
在本發明之第一變體中，兩個膨脹機器耦合至發電機或耗散制動器。較佳地使用發電機渦輪機。儘管此不使任何能量直接返回至程序，但此變體相對於不同負載情況尤其靈活。
較不靈活但更具成本效益的係根據本發明之方法之第二變體，其中兩個膨脹機器各驅動壓縮器級，且在兩個壓縮器級中循序壓縮程序流。替代地，僅兩個渦輪機之一者(例如壓縮氮渦輪機或「第二膨脹機器」)可耦合至壓縮器級，且另一者(例如殘餘氣體渦輪機或「第一膨脹機器」)可耦合至發電機。
此程序流可(例如)由下列流之一者組成：
- 純化之供給空氣之至少一部分，其接著被引入至兩個壓縮器級之下游之主熱交換器中。
- 第一及/或第二加壓氮產品流之至少一部分，其接著被排出作為兩個壓縮器級之下游之加壓氮產品。
原則上，可將冷凝器-蒸發器兩者設計成習知浴槽蒸發器。
然而，較佳地，在其蒸發側上將低壓塔頂部冷凝器設計成強制流動蒸發器。此未產生蒸發側上之流體靜壓力之損耗但產生冷凝側上之相對較低壓力。
替代地或另外，在其蒸發側上將主冷凝器設計成強制流動蒸發器。與浴槽蒸發器相比，此產生蒸發側上之流體靜壓力之較低損耗且亦產生冷凝側上之相對較低壓力。
在本發明之另一實施例中，在第一操作模式中，在壓力下蒸發冷凝氮之至少一部分且接著獲得該至少一部分作為加壓氮產品。使用外部熱量來操作對應蒸發器件，即，明確而言，熱源並非低溫分離系統之程序流。 在第二操作模式中，無冷凝氮或僅小於第一操作模式中之量(例如小於50%)在蒸發器件中蒸發。明確而言，蒸發器件具有空氣加熱蒸發器、水浴蒸發器及/或固體材料冷藏庫。
本發明亦關於一種根據專利技術方案14之用於藉由低溫分離空氣來製造加壓氮及液態氮的器件。根據本發明之裝置可由對應於個別、複數個或全部附屬方法技術方案之特徵的裝置特徵互補。
舉例而言，根據本發明之方法使用下列壓力及溫度：操作壓力(在各情況中於塔之頂部處)：高壓塔：例如12巴至17巴，較佳為13巴至15巴
低壓塔：例如6巴至10巴，較佳為7巴至9巴
低壓塔頂部冷凝器：蒸發空間：例如2巴至5巴，較佳為3巴至4巴
空氣壓力：兩個渦輪機(膨脹機器)之入口溫度：
「第一中間溫度」(殘餘氣體渦輪機)：例如160K至120K，較佳為150K至130K
「第二中間溫度」(氮渦輪機)：例如220K至180K，較佳為210K至190K
在圖1中，藉由具有後冷器3(及中間冷卻(圖中未展示))之主空氣壓縮器2經由過濾器1來將全部供給空氣(AIR)壓縮至約14.6巴之壓力。後續預冷卻系統具有直接接觸冷卻器4。將預冷卻供給空氣5供給至純化器件6(較佳為可切換分子篩子吸附器)。
管線7將全部純化之供給空氣(除相對較小分支(例如用於儀表空氣)之 外)傳送至主熱交換器8，其中純化之供給空氣在至冷端之路徑上被冷卻。將冷的、完全或幾乎完全氣態空氣8引入至高壓塔9中。高壓塔9係亦含有低壓塔10、主冷凝器11及低壓塔頂部冷凝器12之蒸餾塔系統的部分。冷凝器-蒸發器11、12兩者在其等蒸發側上被設計成強制流動蒸發器。
來自高壓塔9之集液槽之液態粗氧13係在逆流過冷器14中冷卻，且係經由管線15供給至低壓塔10之中間點。排出高壓塔9之氣態頂部氮16之第一部分17作為第一加壓氮流且將其供應至主熱交換器8。在主冷凝器11之冷凝空間中至少部分地冷凝氣態頂部氮16之第二部分20。將所得液態氮21之第一部分用作高壓塔9中之再循環流。在逆流過冷器14中冷卻餘料22/23且將其供給至低壓塔10之頂部。
在逆流過冷器14中冷卻來自低壓塔之集液槽或來自主冷凝器11之冷凝空間之液態富氧餾分24且將其作為冷卻劑流經由管線25供給至低壓塔頂部冷凝器12之蒸發空間，於其中液態富氧餾分24至少部分地蒸發。低壓塔頂部冷凝器12之蒸發空間中所製造之蒸氣被排出作為殘餘氣體流26且在主熱交換器8中被加熱至第一中間溫度(例如)142K。在第一中間溫度將殘餘氣體流27供給至第一膨脹機器28(在此情況中採用發電機渦輪機之形式)中，其中殘餘氣體流27依功執行方式膨脹至僅高於大氣壓。在主熱交換器8中完全加熱依功執行方式膨脹之殘餘氣體流29，即，將其加熱至大概環境溫度。
可經由管線31將溫熱殘餘氣體30直接洩流至環境大氣(ATM)。替代地或部分地，可在再生氣體加熱器33中加熱之後經由管線32將溫熱殘餘氣體30用作純化器件6中之再生氣體。經由管線34將用過的再生氣體洩流至環境大氣。
排出來自低壓塔10之氣態頂部氮之第一部分44作為第一加壓氮流，在主熱交換器8中加熱且排出(18,19)作為第一加壓氮產品(PGAN)。在低壓塔頂部冷凝器12之冷凝空間中至少部分地冷凝低壓塔10之氣態頂部氮之第二部分45。排出低壓塔頂部冷凝器12中冷凝之氮46之部分47作為液態氮產品(PLIN)。
在主熱交換器8中將來自高壓塔9之第二加壓氮流17加熱至第二中間溫度207K。在第二中間溫度，將第二加壓氮流40供給至第二膨脹機器41中，於其中依功執行方式將其膨脹至約低壓塔10之頂部處的操作壓力。此處，亦將第二膨脹機器41設計成發電機渦輪機。在主熱交換器中完全加熱依功執行方式膨脹之第二加壓氮流42。溫熱之第二加壓氮流43與溫熱之第一加壓氮流18結合且經由管線19與第一加壓氮產品一起排出作為第二加壓氮產品(PGAN)。
圖2及圖3兩者之方法不同於圖1，其在於：其等將渦輪機處執行之功用於壓縮程序流。此藉由分別耦合至渦輪機28及41且彼此串聯連接且各具有後冷器71、73之兩個壓縮器級(加力器)70、72實現。在此內文中，代替所展示之組態，亦可反向連接壓縮器及渦輪機，即，第一膨脹機器41耦合至第一壓縮器級70且第二膨脹機器41耦合至第二壓縮器級72。
視情況，可將來自高壓塔9之第二加壓氮流17之部分50供給遠至主熱交換器8之暖端且可在13至14巴之壓力洩流作為高壓產品HPGAN(圖中未展示)。
在圖2中，全部空氣7A、7B之壓縮之部分藉由此等渦輪機驅動之壓縮器級70、72執行。例如，主空氣壓縮器需要將此壓縮成僅12.5巴。相應地，主壓縮器可具有較少級。
相比而言，在圖3中，透過壓縮器級70、72發送全部加壓氮產品19A、19B。此允許產品壓力自約8巴升高至約11巴，其中無需供應能量。因此，此亦轉譯成比使用外部驅動氮壓縮器節省成本。
除其中抵著蒸發氮流415/416來使自低壓塔10排出之液態氮47過冷卻之額外逆流過冷器414之外，圖4相同於圖1。為此，經由閥417使該過冷之液態氮之小部分分支。將蒸發之氮416與來自殘餘氣體渦輪機28之排放氣體29混合且在主熱交換器8中將蒸發之氮416與來自殘餘氣體渦輪機28之排放氣體29一起加熱。
另外，與圖1相比，圖5含有純氧塔550，其之集液槽製造經由管線551排出且作為高純度液態氧產品HLOX獲得之高純度液態氧。經由管線552自低壓塔10排出無低揮發性組分之氧氣餾分。其在純氧塔550之集液槽蒸發器553中過冷卻且經由管線554及節流閥555發送至純氧塔550之頂部。此處，分離具有較高程度揮發性之組分。此外，使用來自高壓塔9之氣態頂部氮16之部分556來加熱集液槽蒸發器553；將所得液態氮557發送至低壓塔10。將來自純氧塔550之頂部之非純氣態氧558與殘餘氣體渦輪機28之上游之殘餘氣體26混合。
在低壓塔頂部冷凝器12之蒸發空間中之相對較低壓力(例如，低於3巴)的情況中，宜進行額外措施，例如依可接受點在設備中富集丙烷，及處置來自整流器系統之富集液體(例如在釋放至環境大氣之前處置至噴射器、至周圍環境中或至非純氮流中)。接著，可藉由使用阻擋板直接在高壓塔中依熟知方式進行富集。
由於相對較高液體產量，所以已在至高壓塔之入口處預冷凝空氣(例如，至約1%或更多之程度)。接著在集液槽中分離歸因於此預冷凝而出現 之液體且將該液體與沖洗液體一起棄置。然而，此實質上減小該方法之效率，此係因為，其浪費許多冷氣及許多氮分子。
可在圖6之方法(其依其他方式亦基於圖1之程序)中找到此問題之解決方案。藉由針對來自高壓塔9之高壓塔沖洗液體661使用輔助塔660，可大幅減少接著經由管線662排出之沖洗量。
高壓塔具有一至五個實用板作為阻擋板663。高於阻擋板排出液態粗氧13且在下方(即，直接自集液槽)排出高壓塔沖洗液體661；其含有來自高壓塔或來自阻擋板之再循環液體及經由管線8引入之預冷凝空氣兩者。將流661供給至輔助塔660之頂部(可在過冷卻之後)，在塔內交換材料期間於低揮發組分中富集流661，且最終經由管線662自輔助塔660之集液槽排出(實質上較小量)流661。排出量係(例如)約40至50Nm3/h；相對而言，用於100000Nm3/h之總空氣量之流量662至661之比率係(例如)介於1%與10%之間。使用來自高壓塔9之氣態空氣665來加熱輔助塔660之集液槽蒸發器664。將集液槽蒸發器664中冷凝之空氣666供給至低壓塔10。亦將輔助塔660中所製造之頂部氣體667供給至低壓塔10之適當點。
自空氣部分流665至輔助塔660之冷凝器之C3H8保持於系統中。然而，與供給空氣量相比，此空氣量相對較小(約1%)，且因此操作可靠性藉此未受影響。藉由現自輔助塔660取得沖洗量662的事實，可將再循環量增加至高壓塔中之阻擋區段663。因此，沖洗出更多氙氣且亦可進一步使用及處理來自輔助塔之實際沖洗量662作為氙氣濃縮物；在根據圖6之方法中，氙氣產率可高於50%。
背離圖6中之描繪，可在逆流過冷器14中過冷卻高壓塔沖洗液體661。亦可在來自集液槽蒸發器664之液體流供給至低壓塔10之前在逆流 過冷器14中過冷卻該液體流。
圖7不同於圖6，其在於：在液態時未棄置沖洗流662。反而，經由管線762將沖洗流662供給至其中沖洗流662突然蒸發之溫熱殘餘氣體管線763且接著將其高度稀釋且洩流至環境大氣中。
迄今所描述之方法在具有相對較低液體產量之操作情形中僅具有受限靈活度(即，背離設計情形)。此等情況引起上層冷凝器之蒸發空間中之壓力減小，且因此亦引起至殘餘氣體渦輪機中之入口壓力減小及可行下游後壓縮器之情況中之攝入壓力減小；此尤其關於使用混合天然氣以調整發熱值。然而，後壓縮器之顯著減小之攝入壓力對機器之尺寸量定具有顯著影響且亦對正常欠載行為加以限制。
此情形之相對具成本效益且又相對有效的解決方案可關於圖8中所展示之系統。在具有減小之液體輸出之第一操作模式中，設備中之液體產量未顯著減小，但相反，用過的分離或冷凝能量之部分自液體恢復。此可藉由使用空氣或蒸氣加熱緊急供應蒸發器或藉由連接一或多個冷藏庫來實現。在後一情況中，亦(例如)為了增加其他操作情形中之液體產量之目的而儲存冷凝程序之冷氣之部分。在該第一操作模式(洩流階段)中，亦可使空氣部分流冷凝。
在洩流階段中，減小主空氣壓縮器之功率或(若干)氮產品壓縮器之功率，或替代地，此等保持不變且獲得更多氣體產品。當然，可組合使用此等措施之兩者或三者。
尤其在相對較高產品輸出壓力或中間壓力的情況中，可適宜採用此解決方案，此係因為：隨著增加之壓力根據產品壓縮器處之壓縮器功率之節省更高。
在第二操作模式中，蒸發較少液體產品或不蒸發液體產品。例如，放棄第一操作模式中所使用之此等額外方法步驟。
與圖1相比，在圖8中，在殘餘氣體渦輪機28中膨脹之流之部分830被噴射至環境大氣(ATM)中之前單獨加熱部分830。來自低壓塔10之氮產品44、18在其經由管線819經洩流為加壓產品之前藉由兩個兩級(820，821)氮產品壓縮器而在溫暖環境中進一步被壓縮。產品壓縮器820、821作為整體因此具有四個級。(替代地，亦可與一個、三個或更多級一起使用一或三個氮產品壓縮器。)可將全部壓縮流帶至最後壓力，或替代地，可在中間壓力在兩個氮產品壓縮器820、821之間萃取(圖中未展示)部分壓縮流。
液態氮47之至少部分儲存於液態氮槽870中。較佳地，此液態氮槽870亦用於輸出液體產品(圖8中未展示)。在該第一操作模式中，液態氮871藉由泵浦872來升高壓力(例如約為兩個氮產品壓縮器820與821之間的壓力)；替代地，泵浦輸出處於第一氮產品壓縮器820之壓力上游處或第二氮產品壓縮器821之壓力下游處(圖中未展示)。高壓氮在環境大氣蒸發器873中蒸發；替代地，亦可使用蒸氣加熱水浴蒸發器。經由管線875a、875b、875c將氣體高壓氮與來自低壓塔10之溫熱氣態氮18混合。
在第二操作模式中，關閉環境大氣蒸發器873且輸出整個液體產品PLIN作為端產品或儲存於液態氮槽870中。
1:過濾器
2:主空氣壓縮器
3:後冷器
4:冷卻器
5:供給空氣
6:純化器件；純化
7:管線；供給空氣
7A:空氣；程序流
8:主熱交換器
9:高壓塔
10:低壓塔
11:主冷凝器
12:低壓塔頂部冷凝器
13:液態粗氧
14:逆流過冷器
15:管線
16:氣態頂部氮
17:第二加壓氮流
18:第一加壓氮產品
19:第一加壓氮產品/第二加壓氮產品；管線；共同加壓氮產品流
20:第二部分
21:液態氮
22:餘料
23:餘料
24:液態富氧餾分
25:管線；液態冷卻劑流
26:殘餘氣體流
27:殘餘氣體流
28:第一膨脹機器
29:殘餘氣體流
30:溫熱殘餘氣體
31:管線
32:管線
33:再生氣體加熱器
34:管線
40:第二加壓氮流
41:第二膨脹機器
42:第二加壓氮流
43:第二加壓氮產品；第二加壓氮流
44:第一部分；氮產品；第一加壓氮流
45:第二部分
46:氮
47:液態氮；冷凝氮；部分
552:管線；氧氣餾分
664:集液槽蒸發器
871:液態氮；部分
872:泵浦/升高壓力
873:環境大氣蒸發器/蒸發器件

Claims (15)

  1. 一種用於製造加壓氮及液態氮之方法，其藉由低溫分離蒸餾塔系統中之空氣，該蒸餾塔系統具有高壓塔(9)及低壓塔(10)及兩者被設計成冷凝器-蒸發器之主冷凝器(11)及低壓塔頂部冷凝器(12)，其中供給空氣流(AIR)係於主空氣壓縮器(2)中壓縮，被純化(6)，在主熱交換器(8)中冷卻且經由管線(8')被引入至該高壓塔(9)中，來自該低壓塔(10)之該氣態頂部氮之第一部分(44)被排出作為第一加壓氮流，在該主熱交換器(8)中被加熱且被排出作為第一加壓氮產品(18,19,PGAN)，該低壓塔(10)之該氣態頂部氮之第二部分(45)至少部分地在該低壓塔頂部冷凝器(12)之冷凝空間中冷凝，液態冷卻劑流(25)至少部分地在該低壓塔頂部冷凝器(12)之蒸發空間中蒸發，該低壓塔頂部冷凝器(12)之該蒸發空間中所製造之蒸氣被排出作為殘餘氣體流(26)且在該主熱交換器(8)中被加熱至第一中間溫度，在該第一中間溫度之該殘餘氣體流(27)被引入至第一膨脹機器(28)中，於其中該殘餘氣體流(27)依功執行方式膨脹，及在該主熱交換器(8)中完全加熱依功執行方式膨脹之該殘餘氣體流(29)，其特徵在於第二加壓氮流(17)自該高壓塔(9)之頂部排出且在該主熱交換器(8)中被加熱至第二中間溫度， 將在該第二中間溫度之該第二加壓氮流(40)引入至第二膨脹機器(41)中，於其中該第二加壓氮流(40)依功執行方式膨脹，在該主熱交換器(8)中完全加熱依功執行方式膨脹之該第二加壓氮流(42)且將其排出作為第二加壓氮產品(43，19，PGAN)，及將該低壓塔頂部冷凝器(12)中冷凝之氮(46)之部分(47)排出作為液態氮產品(PLIN)。
  2. 如請求項1之方法，其中在8.0巴至9.0巴之壓力下自該低壓塔(10)之頂部排出該第一加壓氮流(44)。
  3. 如請求項1或2之方法，其中依功執行方式膨脹之該第二加壓氮流(42，43)與該第一加壓氮流(44,18)結合，且排出該第一加壓氮產品及該第二加壓氮產品作為共同加壓氮產品流(19，PGAN)。
  4. 如請求項1或2之方法，其中該第二中間溫度高於該第一中間溫度至少10K。
  5. 如請求項1或2之方法，其中該第一膨脹機器及該第二膨脹機器(28，41)耦合至發電機或耗散制動器。
  6. 如請求項1或2之方法，其中該兩個膨脹機器(28，41)各驅動壓縮器級(70，72)，其中在該兩個壓縮器級中循序壓縮程序流(7A，19A)。
  7. 如請求項6之方法，其中該程序流由引入至該兩個壓縮器級(70，72)之下游之該主熱交換器(8)中之該純化之供給空氣(7A)之至少一部分組成。
  8. 如請求項6之方法，其中該程序流由經排出作為該兩個壓縮器級之下游之加壓氮產品(19B，PGAN)之該第一及/或第二加壓氮產品流(19A)之至少一部分組成。
  9. 如請求項1或2之方法，其中該低壓塔頂部冷凝器(12)在其蒸發側上被設計成強制流動蒸發器。
  10. 如請求項1或2之方法，其中該主冷凝器(11)在其蒸發側上被設計成強制流動蒸發器。
  11. 如請求項1或2之方法，其中氧氣餾分(552)自該低壓塔(10)排出且被供給至純氧塔(550)，其中高純度液態氧產品自該純氧塔(550)之集液槽排出，且明確而言，該純氧塔具有使用該氧氣餾分(552)之至少一部分及/或使用來自該高壓塔(9)之頂部之氣態氮(556)來加熱之集液槽蒸發器。
  12. 如請求項1或2之方法，其中高壓塔沖洗液體(661)自該高壓塔排出且被引入至具有集液槽蒸發器(664)之輔助塔(660)中，明確而言，該集液槽蒸發器(664)使用空氣部分流(665)來加熱，其中自該輔助塔(660)之集液槽蒸發器(664)取得沖洗流且將其棄置或發送用於氙提取。
  13. 如請求項1或2之方法，其中在第一操作模式中，該冷凝氮(47)之至少一部分(871)在液態中達到升高壓力(872)，在使用外部熱來操作之蒸發器件(873)中蒸發，及接著被獲得作為加壓氮產品(874，819)，且在第二操作模式中，無冷凝氮(47)或小於該第一操作模式中之量在使用外部熱來操作之該蒸發器件(873)中蒸發，其中使用外部熱來操作之該蒸發器件(873)具有，明確而言，空氣加熱蒸發器，水浴蒸發器及/或固體材料冷藏庫。
  14. 如請求項1或2之方法，其中在8.4巴至9.0巴之壓力下自該低壓塔(10)之頂部排出該第一加壓氮流(44)。
  15. 一種用於藉由低溫分離空氣來製造加壓氮及液態氮之裝置，其具有蒸餾塔系統，其具有高壓塔(9)及低壓塔(10)及兩者經設計成冷凝器-蒸發器之主冷凝器(11)及低壓塔頂部冷凝器(12)，主空氣壓縮器(2)，其用於壓縮供給空氣流(AIR)，純化器件(6)，其用於純化該壓縮之供給空氣(5)，主熱交換器(8)，其用於冷卻該純化之供給空氣(7)，用於將該冷卻之供給空氣經由管線(8')引入至該高壓塔(9)中之構件， 用於排出來自該低壓塔(10)之該氣態頂部氮之第一部分(44)作為第一加壓氮流之構件，用於在該主熱交換器(8)中加熱該第一加壓氮流之構件，用於排出該加熱之第一加壓氮流作為第一加壓氮產品(18，19，PGAN)之構件，用於將來自該低壓塔(10)之該氣態頂部氮之第二部分(45)供給至該低壓塔頂部冷凝器(12)之冷凝空間中之構件，用於將液體冷卻劑流(25)供給至該低壓塔頂部冷凝器(12)之蒸發空間中之構件，用於排出該低壓塔頂部冷凝器(12)之該蒸發空間中所製造之蒸氣作為殘餘氣體流(26)之構件，用於將該殘餘氣體流(26)供給至該主熱交換器中之構件，用於在第一中間溫度將該殘餘氣體流(27)自該主熱交換器(8)排出之構件，第一膨脹機器(28)，其用於功執行膨脹加熱至該第一中間溫度之該殘餘氣體流(27)，及具有用於在該主熱交換器(8)中完全加熱依功執行方式膨脹之該殘餘氣體流(29)之構件，其特徵在於用於排出來自該高壓塔(9)之頂部之第二加壓氮流(17)之構件，用於將該主熱交換器(8)中之該第二加壓氮流(17)加熱至第二中間溫度之構件，用於在該主熱交換器(8)中完全加熱依功執行方式膨脹之該第二加壓 氮流(42)之構件，用於排出該加熱之第二加壓氮流作為第二加壓氮產品(43，19，PGAN)之構件，及用於排出該低壓塔頂部冷凝器(12)中冷凝之氮(46)之部分(47)作為液態氮產品(PLIN)之構件。
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