TW201607598A - 以可變能耗低溫分離空氣之方法與裝置 - Google Patents
以可變能耗低溫分離空氣之方法與裝置 Download PDFInfo
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- TW201607598A TW201607598A TW104121751A TW104121751A TW201607598A TW 201607598 A TW201607598 A TW 201607598A TW 104121751 A TW104121751 A TW 104121751A TW 104121751 A TW104121751 A TW 104121751A TW 201607598 A TW201607598 A TW 201607598A
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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
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04018—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 main feed 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
- F25J3/04012—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
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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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- F25J3/04078—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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- 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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- 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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- F25J3/04175—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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- 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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- 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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- 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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- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
- F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
Abstract
該方法及該裝置係在蒸餾塔系統中藉低溫分離空氣來可變提取壓縮氣體產品(72;73),該蒸餾塔系統具有高壓塔(21)及低壓塔(22)。全部之所用空氣在主空氣壓縮機(2)中被壓縮至第一壓力,該第一壓力比該高壓塔(21)之操作壓力高至少4bar。在該主空氣壓縮機(2)中被壓縮之所用空氣(7)的第一分流(8,11,14)在主熱交換器(13)中冷卻至中間溫度並在第一空氣渦輪機(15)中膨脹做功並被導入(40;18,19,20)該蒸餾塔系統。在該主空氣壓縮機(2)中被壓縮之所用空氣的第二分流(12,27,29,30)在第一增壓壓縮機(9)中被再壓縮,在該主熱交換器(13)中冷卻,而後膨脹(31)並被導入該蒸餾塔系統。自該蒸餾塔系統液態提取第一產品流(69;75),將其增壓(71;76)至第一產品壓力,在該主熱交換器(13)中蒸發或假蒸發並加熱該第一產品流並將其作為第一壓縮氣體產品(GOX IC;GAN IC)加以提取。來自該低壓塔之氣態氮(55,56)在多級氮產品壓縮機(57/59)中由入口壓力壓縮至最後壓力。來自該高壓塔(21)之氣態氮(178,179,180)在該氮壓縮機(57/59)之第一級下游至少間歇性地與該來自該低壓塔之氮混合。在第一操作模式下提取第一壓縮氣體產品之第一量並且在第二操作模式下提取第二量,該第二量小於該第一量。在該第一操作模式下在該氮壓縮機(57/59)中壓縮高壓塔氮(178,179,180)之第一量,該第一量亦可為
零,並且在該第二操作模式下壓縮第二量,該第二量大於該第一量。
Description
本發明係有關一種藉低溫分離空氣來可變提取(variable Gewinnung)壓縮氣體產品之方法與裝置。
用於低溫分離空氣之方法與裝置例如披露於Hausen/Linde,Tieftemperaturtechnik,2.Auflage 1985,Kapitel 4(Hausen/Linde,低溫技術,1985年第2版,第4章,第281至337頁)。
此類設備之蒸餾塔系統可構造成雙塔系統(例如經典Linde雙塔系統),或者亦可構造成三塔或多塔系統。除氮氧分離塔外,該系統還可具有用於提取高純度產品及/或其他空氣組分特別是稀有氣體之其他裝置,例如提氬裝置及/或氮氙提取裝置。
在製程中的“內壓縮”階段,在液態下被加壓之產品流遇熱載體而蒸發且最終作為經內壓縮之壓縮氣體產品被提取。此方法亦稱內壓縮。其用於提取氣態加壓產品。在超臨界壓力下不發生真正意義上之相變,遂使得產品流“假蒸發”。該產品流例如可為來自雙塔系統之低壓塔的氧產品或者來自雙塔系統之高壓塔或主冷凝器(高壓塔與低壓塔透過該主冷凝器而處於熱交換連接)之液化室的氮產品。
處於高壓下之熱載體遇該(假)蒸發產品流而液化(若熱載體處於超臨界壓力下,則為假液化)。該熱載體往往由空氣的一部分構成,在該情況下由經壓縮之所用空氣的“第二分流”構成。
內壓縮方法例如披露於DE 830805、DE 901542(=US 2712738/US 2784572)、DE 952908、DE 1103363(=US 3083544)、DE
1112997(=US 3214925)、DE 1124529、DE 1117616(=US 3280574)、DE 1226616(=US 3216206)、DE 1229561(=US 3222878)、DE 1199293、DE 1187248(=US 3371496)、DE 1235347、DE 1258882(=US 3426543)、DE 1263037(=US 3401531)、DE 1501722(=US 3416323)、DE 1501723(=US 3500651)、DE 253132(=US 4279631)、DE 2646690、EP 93448 B1(=US 4555256)、EP 384483 B1(=US 5036672)、EP 505812 B1(=US 5263328)、EP 716280 B1(=US 5644934)、EP 842385 B1(=US 5953937)、EP 758733 B1(=US 5845517)、EP 895045 B1(=US 6038885)、DE 19803437 A1、EP 949471 B1(=US 6185960 B1)、EP 955509 A1(=US 6196022 B1)、EP 1031804 A1(=US 6314755)、DE 19909744 A1、EP 1067345 A1(=US 6336345)、EP 1074805 A1(=US 6332337)、DE 19954593 A1、EP 1134525 A1(=US 6477860)、DE 10013073 A1、EP 1139046 A1、EP 1146301 A1、EP 1150082 A1、EP 1213552 A1、DE 10115258 A1、EP 1284404 A1(=US 2003051504 A1)、EP 1308680 A1(=US 6612129 B2)、DE 10213212 A1、DE 10213211 A1、EP 1357342 A1或DE 10238282 A1DE 10302389 A1、DE 10334559 A1、DE 10334560 A1、DE 10332863 A1、EP 1544559 A1、EP 1585926 A1、DE 102005029274 A1 EP 1666824 A1、EP 1672301 A1、DE 102005028012 A1、WO 2007033838 A1、WO 2007104449 A1、EP 1845324 A1、DE 102006032731 A1、EP 1892490 A1、DE 102007014643 A1、A1、EP 2015012 A2、EP 2015013 A2、EP 2026024 A1、WO 2009095188 A2或DE 102008016355 A1。
DE 102010052545 A1揭露一種在主熱交換器中加熱空氣流並將其回輸至主空氣壓縮機之穩態內壓縮方法。
該發明具體係關於將全部之所用空氣壓縮至一壓力的系統,該
壓力大幅超過蒸餾塔系統之塔內部佔優勢的最高蒸餾壓力(正常情況下為高壓塔壓力)。此類系統亦稱HAP製程(HAP-high air pressure,高空氣壓力)。其中,“第一壓力”即用以壓縮總空氣之主空氣壓縮機(MAC=main air compressor)的出口壓力例如超過最高蒸餾壓力4bar以上,特定言之超過最高蒸餾壓力6bar至16bar。“第一壓力”之絕對值例如介於17bar與25bar間。在HAP法中,主空氣壓縮機通常為唯一一台由外部供能之空氣壓縮機器。“唯一一台機器”係指所有級皆連接同一驅動裝置之單級或多級壓縮機,其中所有級皆安置在同一殼體內或連接同一傳動裝置。
所謂的MAC-BAC法為上述HAP法之替代方案,其在主空氣壓縮機內將空氣壓縮至較低之總空氣壓力,例如壓縮至高壓塔之操作壓力(加上管線損失)。來自主空氣壓縮機之空氣的一部分在由外部供能之增壓空氣壓縮機(BAC=booster air compressor)內被壓縮至更高壓力。此部分處於更高壓力下之空氣(通常稱為節制流)在主熱交換器中提供內壓縮產品(假)蒸發所需要之絕大部分熱。此部分空氣於主空氣壓縮機下游在節流閥或密集液體膨脹機(DLE=dense liquid expander)內膨脹至蒸餾塔系統所需之壓力。
由於對內壓縮產品的需求存在波動,要求將空氣分離設備設計成能以可變運行來實現可變之壓縮氣體生產。反之,有益者係空氣分離設備在生產恆定或基本恆定之情況下仍設置能耗不同之不同操作模式以實現可變運行。
此種邊界條件之一具體實例係為在環氧乙烷生產設備上提供內壓縮氧(GOXIV)及視情況其他氣態及/或液態產品。在此,需氧量往往與生產EO時之觸媒狀態相匹配;故該需氧量在觸媒壽命(一般3年左右)期間可能在100%與約70%間變化。其要點在於,在此期間空氣分離設備大約以相同時間形成不同之GOXIV產品數量(介於100%與約
70%間)。因此,設備既在設計情況下以100%GOXIV運行,亦在欠載情況下高效運行,此點較為重要。此要求由於以下因素而進一步加大難度:其他空分產品之生產不受GOXIV產品影響;例如當GOX生產由100%下降至約70%時,對一種、數種或所有其他空分產品之需求可能保持不變。此等“其他空分產品”例如可為以下產品中的一種、數種或全部:
- 內壓縮氮產品(GANIV)
- 其他氣態加壓產品,例如氣態提取自高壓塔且視情況而在氮氣壓縮機內經進一步壓縮之加壓氮(HPGAN)。
- 液態產品如液氧、液氮及/或液氬。
採用傳統MAC-BAC法能較好地實現此項任務,因為兩壓縮機(MAC及BAC)分管不同功能之任務。主空氣壓縮機基本僅提供分離所用之空氣;增壓空氣壓縮機為內壓縮(GOXIV,GANIV)及液體生產供能。兩機器通常在70%與100%間較易控制。
HAP法使用唯一一台壓縮機來解決此兩項任務(提供待分離空氣以及為內壓縮及/或液體生產供能)。此會導致某些工況處於壓縮機特性曲線族以外且無法加以操縱之情形。空氣分離設備之整體能量需求並非僅取決於GOXIV產品,而是絕大部分取決於液體生產及其他內壓縮產品。但待分離空氣之量往往取決於GOXIV產品。若GOXIV量顯著減少,則被送入設備之待分離空氣的量亦明顯減少。如此一來,輸入系統之能量亦大幅減少,從而可能不足以用來如願生產其他產品(液體、GANIV等等)。為了在空氣量明顯減少之情況下仍能提供足夠多的能量,須大幅提高壓縮機壓力。但HAP法僅在有限範圍內能實現此點,因為a)機器特性曲線族受限,以及b)設備“熱”部(預冷裝置、吸附器等等)之設計壓力不得被超
過。
本發明之目的在於提供一種方法及一種相應之裝置,其將HAP法之優點與MAC-BAC法之靈活性相結合。“靈活性”在此具體指系統並非僅在內壓縮產品之特定生產量下可節能運行,而是可在較寬之負載範圍內以大體恆定之較低專用能耗運行。其中具體而言,其他空分產品之生產應保持不變或者其變化強度至少應小於內壓縮產品之產品數量的變化強度。
請求項1之特徵為本發明用以達成該目的之解決方案。
本發明在第二操作模式下導引氮富集製程流(“第二製程流”)從低壓塔旁邊流過。
根據本發明,在高壓塔中提取之氮的一部分不被導入低壓塔,而是被回輸至氮產品壓縮機,具體實現方式為:- 多級壓縮機由氮產品壓縮機構成,- 第一製程流由來自低壓塔之第一氣態氮流構成,並且- 第二製程流由來自高壓塔之第一氣態氮流構成。
若在製程中例如由於氮產品數量大而設置低壓GAN壓縮機作為氮產品壓縮機(尤其在內壓縮GAN產量較大之情況下),則可藉由中間饋送來自高壓塔之加壓GAN來為該低壓GAN壓縮機去負荷。與設計情況不同,GOXIV產量減小時送入精餾系統之空氣及提取自加壓塔之加壓GAN皆遠多於製氧所需之量。此加壓GAN在熱交換器中加熱後於合適位置處(例如在第二或第三壓縮機級之後)被送入氮產品壓縮機。藉此可相應減小低壓GAN(有待大體由大氣壓力壓縮至5bar左右之氣體量)之份額。例如在約75%GOXIV、完全液體生產及100%HPGAN產品數量之工況(不同於100%GOXIV之設計情況)下,約70-75%低壓GAN及約25-30%來自加壓塔之加壓GAN得到壓縮。藉此可部分回收在主空氣壓縮機上利用過剩空氣量所吸收之能量。
第二製程流原則上亦可在氮產品壓縮機之入口處與第一製程流混合。但在許多情況下,有益者係使第二製程流在多級氮產品壓縮機之中間級與第一製程流混合。
進一步地,在第二操作模式下可自低壓塔下部區域提取氧氣流,將該氧氣流與來自低壓塔上部區域之氮富集流混合並且在主熱交換器中加熱該混合物。
根據本發明之特殊實施方式,此外更可使用第二空氣渦輪機,其中在主空氣壓縮機中被壓縮之所用空氣的第三分流在主熱交換器中冷卻至中間溫度並在該第二空氣渦輪機中膨脹做功,並且該經膨脹做功之第三分流的至少一第一部分被導入蒸餾塔系統。
此外,在主空氣壓縮機中被壓縮之所用空氣的第二分流可在主熱交換器中冷卻至中間溫度,在作為冷壓縮機運行且由第二渦輪機驅動之第二增壓壓縮機中被再壓縮至高於第一壓力之第三壓力,在主熱交換器中冷卻,(假)液化,而後膨脹並被導入蒸餾塔系統。藉此方式可在不耗用外部能量之情況下進一步提高第二分流之壓力。可達到相應更高之內壓縮壓力。
進一步地,在主空氣壓縮機中被壓縮之空氣的第四分流可在第一壓力下在主熱交換器中冷卻,而後膨脹並被導入蒸餾塔系統。此種第二節制流有助於進一步最佳化主熱交換器中之熱交換程序。
在包含第二渦輪機之另一實施方式中,有利地,第三分流在第二空氣渦輪機中膨脹至一壓力,該壓力比高壓塔之操作壓力高至少1har,並且經膨脹做功之第三分流在主熱交換器中進一步冷卻,而後膨脹並被導入蒸餾塔系統。此種第三節制流有助於進一步最佳化主熱交換器中之熱交換程序。
本發明方法特定言之在由第一操作模式切換至第二操作模式時,在主空氣壓縮機中被壓縮之總空氣量根本不減少或者減少程度小
於加壓氧產品數量,具體實現方式為:- 在第一操作模式下在主空氣壓縮機中壓縮所用空氣之第一量,並且- 在第二操作模式下在主空氣壓縮機中壓縮所用空氣之第二量,其中- 所用空氣之第二量與所用空氣之第一量之比大於第一壓縮氣體產品之第二量與第一壓縮氣體產品之第一量之比,特定言之大至少3%,尤其大5%以上。
在GOXIV產量減小之工況下,“人為”提高送入冷箱之所用空氣量,即送入設備低溫部分之空氣量超過提取此工況所要求之加壓氧產品所需要的空氣量。若以“過剩”模式操作所用空氣,則可減小壓縮機出口處之壓力,因為此情況下係利用空氣量而非空氣壓力來為GOXIV產品之(假)蒸發供能。其意義在於不僅只簡單地以“過剩”模式操作空氣(在主空氣壓縮機中被壓縮,在熱交換器中冷卻,在渦輪機中膨脹至高壓塔壓力,在熱交換器中再度被加熱且最終經節流處理而達到大氣壓力),而是透過前述特徵亦能實現其他優點。
透過此措施,仍有足夠的空氣可用來提取其他產品。例如可足量製冷來提供恆定之液體產品數量。
在主空氣壓縮機中被壓縮之所用空氣的第一分流較佳在被導入主熱交換器之前在特定言之由第一渦輪機驅動之熱運行的第一增壓壓縮機中被再壓縮。如此一來,第一渦輪機之入口壓力遠高於總空氣經壓縮而達到之第一壓力。用於第二渦輪機之空氣則例如未經再壓縮,即其入口壓力處於第一壓力之較低水平。
本發明更有關於一種如請求項10之裝置。可用對應於相關方法請求項之特徵的設備特徵補充本發明之裝置。
“用於在第一與第二操作模式間切換之手段”係指能透過共同
作用而在兩操作模式間實現至少部分自動切換的複合型調控裝置,例如經相應程式化之操作控制系統。
下面結合圖式中以示意圖形式示出之實施例詳細闡述本發明及本發明之其他技術細節。
1‧‧‧過濾器
2‧‧‧主空氣壓縮機
3‧‧‧總空氣流
4‧‧‧預冷裝置
5‧‧‧經預冷之總空氣流
6‧‧‧淨化裝置
7‧‧‧經淨化之總空氣流
8‧‧‧第一部分
9‧‧‧增壓空氣壓縮機
10‧‧‧再冷器
11‧‧‧第一分流
12‧‧‧第二分流
13‧‧‧主熱交換器
14‧‧‧經冷卻之第一分流
15‧‧‧第一空氣渦輪機
16‧‧‧經膨脹做功之第一分流
17‧‧‧分離器/氣態分量
18‧‧‧液態分量
19‧‧‧管線
20‧‧‧管線
21‧‧‧高壓塔
22‧‧‧低壓塔
23‧‧‧主冷凝器
24‧‧‧氬提取裝置
25‧‧‧粗氬塔
26‧‧‧精氬塔
27‧‧‧管線
28‧‧‧冷壓縮機
29‧‧‧經再壓縮之第二分流
30‧‧‧冷第二分流
31‧‧‧節流閥
32‧‧‧管線
33‧‧‧部分
34‧‧‧過冷式逆流熱交換器
35‧‧‧管線
36‧‧‧第三分流
37‧‧‧經冷卻之第三分流
38‧‧‧第二空氣渦輪機
39‧‧‧經膨脹做功之第三分流
40‧‧‧管線
41‧‧‧第四分流
42‧‧‧冷第四分流
43‧‧‧節流閥
45‧‧‧管線
46‧‧‧蒸汽
47‧‧‧剩餘液體
48‧‧‧頂部氮
49‧‧‧第一部分
50‧‧‧液氮
51‧‧‧第一部分
52‧‧‧第二部分
53‧‧‧管線
54‧‧‧另一部分
55‧‧‧氣態低壓氮
56‧‧‧熱低壓氮
57‧‧‧第一區段
58‧‧‧中間冷卻裝置
59‧‧‧第二區段
60‧‧‧再冷裝置
61‧‧‧氣態不純氮
62‧‧‧熱不純氮
63‧‧‧排放
64‧‧‧再生氣體
65‧‧‧回輸管線
66‧‧‧回輸管線
67‧‧‧管線
68‧‧‧管線
69‧‧‧液氧
70‧‧‧第一部分
71‧‧‧氧泵
72‧‧‧管線
73‧‧‧第二部分
74‧‧‧管線
75‧‧‧第三部分
76‧‧‧氮泵
77‧‧‧管線
78‧‧‧第二部分
79‧‧‧管線/密封氣體量
178‧‧‧管線
179‧‧‧管線
180‧‧‧附加部分/第二製程流/氮量
181‧‧‧氣態氧/管線
339‧‧‧經膨脹做功之渦輪機流量
340‧‧‧經進一步冷卻之第三分流
341‧‧‧節流閥
436‧‧‧第三分流
圖1為向主空氣壓縮機回輸渦輪機空氣之方法實施例,該方法並非本案請求保護之主題,圖2為本發明將來自高壓塔之氣態氮導入氮產品壓縮機之實施例,及圖3及圖4為圖1之變體,包括第三節制流。
首先結合圖1說明一種方法之實施方式的第一操作模式,該方法並非本案請求保護之主題。主空氣壓縮機2透過過濾器1抽吸大氣空氣(AIR)。該主空氣壓縮機在示例中具有五級並且將總空氣流壓縮至例如為22bar之“第一壓力”。主空氣壓縮機2下游之總空氣流3於第一壓力下在預冷裝置4中冷卻。經預冷之總空氣流5在具體由一對可切換之分子篩吸附器構成的淨化裝置6中被淨化。經淨化之總空氣流7的第一部分8在包含再冷器10之熱運行的增壓空氣壓縮機9中被再壓縮至例如為28bar之第二壓力,而後分成“第一分流”11(第一渦輪機空氣流)及“第二分流”12(第一節制流)。
第一分流11在主熱交換器13中冷卻至第一中間溫度。經冷卻之第一分流14在第一空氣渦輪機15中由該第二壓力膨脹做功至約5.5bar。第一空氣渦輪機15驅動熱增壓空氣壓縮機9。經膨脹做功之第一分流16被導入分離器(相分離器)17。液態分量18由管線19及20送入蒸餾塔系統之低壓塔22。
該蒸餾塔系統包括高壓塔21、低壓塔22、主冷凝器23以及包含粗氬塔25及精氬塔26之常用氬提取裝置24。主冷凝器23構造成冷凝蒸
發器,在具體示例中構造成串級蒸發器。在示例中,高壓塔塔頂之操作壓力為5.3bar,低壓塔塔頂之操作壓力為1.35bar。
所用空氣之第二分流12在主熱交換器13中冷卻至高於第一中間溫度之第二中間溫度,由管線27送入冷壓縮機28並於該處被再壓縮至約為40bar之“第三壓力”。經再壓縮之第二分流29在高於第二中間溫度之第三中間溫度下被再度導入主熱交換器13並於該處冷卻至冷端溫度。冷第二分流30在節流閥31中大體膨脹至高壓塔之操作壓力並由管線32送入高壓塔21。一部分33被再度提取,在過冷式逆流熱交換器34中冷卻並由管線35及20送入低壓塔22。
所用空氣之“第三分流”36在第一壓力下被導入主熱交換器13並於該處冷卻至第四中間溫度,該第四中間溫度在示例中略低於第一中間溫度。經冷卻之第三分流37在第二空氣渦輪機38中由第一壓力大體膨脹做功至高壓塔壓力。第二空氣渦輪機38驅動冷壓縮機28。經膨脹做功之第三分流39由管線40送入高壓塔21底層。
“第四分流”41(第二節制流)在第一壓力下由熱端至冷端貫穿主熱交換器13。冷第四分流42在節流閥43中大體膨脹至高壓塔之操作壓力並由管線32送入高壓塔21。
高壓塔21之氧富集底層液體在過冷式逆流熱交換器34中冷卻並由管線45導入可選之氬提取裝置24。由此產生之蒸汽46及剩餘液體47被送入低壓塔22。
高壓塔21之頂部氮48的第一部分49在主冷凝器23之液化室內遇到在蒸發室內蒸發之低壓塔底層液氧而完全液化或大體上完全液化。其間所產生之液氮50的第一部分51作為回流被送往高壓塔21。第二部分52在過冷式逆流熱交換器34中冷卻並由管線53送入低壓塔22。該液態低壓氮之至少一部分53在低壓塔22中用作回流;另一部分54可作為液氮產品(LIN)被提取。
自低壓塔22頂部提取氣態低壓氮55並在過冷式逆流熱交換器34及主熱交換器13中加熱之。熱低壓氮56在由兩區段構成且包含中間冷卻裝置及再冷裝置(58,60)之氮產品壓縮機(57,59)中被壓縮至期望產品壓力,該期望產品壓力在示例中為12bar。該氮產品壓縮機之第一區段57例如由包含相關再冷器之兩或三級構成;第二區段59具有至少一級且較佳同樣經中間冷卻及再冷卻。
自低壓塔22之中間位置提取氣態不純氮61並在過冷式逆流熱交換器34及主熱交換器13中加熱之。熱不純氮62可排放(63)入大氣(ATM)及/或作為再生氣體64用於淨化裝置6。
管線67及68(所謂的氬通道(Argonübergang))將低壓塔22與氬提取裝置24之粗氬塔25連接起來。
來自低壓塔22底層之液氧69的第一部分70作為“第一產品流”被提取,在氧泵71中達到例如為37bar之“第一產品壓力”並在該第一產品壓力下在主熱交換器13中蒸發,最終透過管線72作為“第一壓縮氣體產品”(GOX IC-內壓縮氣態氧)被提取。
來自低壓塔22底層之液氧69的第二部分73視情況在過冷式逆流熱交換器34中冷卻並且透過管線74作為液氧產品(LOX)被提取。
在示例中,來自高壓塔21或主冷凝器23之液氮50的第三部分75亦經內壓縮處理,具體係該部分在氮泵76中達到例如為37bar之第二產品壓力並在該第二產品壓力下在主熱交換器13中假蒸發,最終透過管線77作為內壓縮氣態氮加壓產品(GAN IC)被提取。
高壓塔21之氣態頂部氮48的第二部分78在主熱交換器中被加熱並且透過管線79或者作為氣態中壓產品被提取,或者-如圖所示-作為密封氣體(Sealgas)用於圖中所示之一或數個製程泵。
若將達到最高製氧率(根據設計為100%)之運行稱作“第一操作模式”,則圖中加粗示出之管線65/66在此運行方式下保持不工作狀
態。
在此情況下,更低之製氧率(例如75%)可被視作“第二操作模式”。在此,經膨脹做功之第一分流16之氣態分量17的一部分作為“第二製程流”由管線65、66經主熱交換器回輸至主空氣壓縮機2之中間級。在示例中,該回輸流在主空氣壓縮機之第二與第三級或第三與第四級間與所用空氣混合。(此所用空氣在此為“第一製程流”。)藉此可使得通過渦輪機15之空氣量保持較高水平並確保所提取之氮產品及液體產品的量不變或者至少減小幅度不大。
95%運行方式可被視作“第一操作模式”。在此情況下,製氧率例如達到設計值之90%時即為“第二操作模式”。
以下表格所列為如圖1之設備之兩種不同操作模式的示例性數值:
表格中之回輸量係關於通過過濾器1之當前空氣量。若無其他規定,則所給出之所有百分比全文皆指莫耳量。
圖2示出本發明之實施方式。其與圖1之區別在於下述特徵;除此之外,關於圖1之描述亦適用於圖2。
此處未設用於空氣之回輸管線65、66。作為替代,在第二操作模式下,除密封氣體量79外,來自高壓塔頂部之氣態頂部氮48的附加部分180作為“第二製程流”180由管線178、179輸送且最終在氮產品壓縮機之兩區段57、59間與來自低壓塔之氮56混合,此氮在該方案中形成“第一製程流”。
來自高壓塔之相應氮量180不在主冷凝器23中冷凝且不被導入低壓塔。在此情況下,此氮量不參加低壓塔中之精餾(既非間接透過底層氧蒸發,亦非直接作為回流液體),從而實現製氧率之減小。與此
同時,等量(或僅略少於此氮量之)空氣可用於製冷與製氮。
在第一操作模式下,更少量之第二製程流180被送往氮產品壓縮機之中間位置或者管線180完全關閉。
透過下文所述之可選措施可進一步提高該方法之靈活性(此項措施基本上亦可應用於圖1所示之方法)。其中在第二操作模式下自低壓塔提取氣態氧181並將其與來自低壓塔之氣態不純氮61混合。示例中係在過冷式逆流熱交換器34下游進行該混合。在第一操作模式下,管線181關閉或者由管線181輸送之氣體有所減少。
以下表格所列為如圖2之設備之兩種不同操作模式的示例性數值:
通過管線180之氮量與設計情況下通過過濾器1之空氣量有關。
圖3與圖1之區別在於第三節制流。為此,第二渦輪機38以較大出口壓力及較高出口溫度運行。在此情況下,經膨脹做功之渦輪機流339的壓力比高壓塔操作壓力高至少1bar,特定言之高4bar至11bar,其溫度比主熱交換器冷端之低壓氮流55、61的入口溫度高至少10K,特定言之高20K至60K。此流而後在主熱交換器之冷部中進一步冷卻。經進一步冷卻之第三分流340作為第三節制流在節流閥341中大體膨脹至高壓塔壓力並由管線32送入高壓塔。藉此可進一步最佳化主熱交換器中之熱交換程序。
圖4不同於圖3之處在於,第三分流436在更高之第二壓力而非在第一壓力下被導入第二渦輪機38。
圖3及圖4之附加措施不僅可用於本發明如圖1所示之變體,亦可用於本發明。
1‧‧‧過濾器
2‧‧‧主空氣壓縮機
3‧‧‧總空氣流
4‧‧‧預冷裝置
5‧‧‧經預冷之總空氣流
6‧‧‧淨化裝置
7‧‧‧經淨化之總空氣流
8‧‧‧第一部分
9‧‧‧增壓空氣壓縮機
10‧‧‧再冷器
11‧‧‧第一分流
12‧‧‧第二分流
13‧‧‧主熱交換器
14‧‧‧經冷卻之第一分流
15‧‧‧第一空氣渦輪機
16‧‧‧經膨脹做功之第一分流
17‧‧‧分離器/氣態分量
18‧‧‧液態分量
19‧‧‧管線
20‧‧‧管線
21‧‧‧高壓塔
22‧‧‧低壓塔
23‧‧‧主冷凝器
25‧‧‧粗氬塔
26‧‧‧精氬塔
27‧‧‧管線
28‧‧‧冷壓縮機
29‧‧‧經再壓縮之第二分流
30‧‧‧冷第二分流
31‧‧‧節流閥
32‧‧‧管線
33‧‧‧部分
34‧‧‧過冷式逆流熱交換器
35‧‧‧管線
36‧‧‧第三分流
37‧‧‧經冷卻之第三分流
38‧‧‧第二空氣渦輪機
39‧‧‧經膨脹做功之第三分流
40‧‧‧管線
41‧‧‧第四分流
42‧‧‧冷第四分流
43‧‧‧節流閥
45‧‧‧管線
48‧‧‧頂部氮
49‧‧‧第一部分
50‧‧‧液氮
51‧‧‧第一部分
53‧‧‧管線
54‧‧‧另一部分
55‧‧‧氣態低壓氮
56‧‧‧熱低壓氮
57‧‧‧第一區段
58‧‧‧中間冷卻裝置
59‧‧‧第二區段
60‧‧‧再冷裝置
61‧‧‧氣態不純氮
62‧‧‧熱不純氮
63‧‧‧排放
64‧‧‧再生氣體
69‧‧‧液氧
71‧‧‧氧泵
72‧‧‧管線
73‧‧‧第二部分
74‧‧‧管線
75‧‧‧第三部分
76‧‧‧氮泵
77‧‧‧管線
78‧‧‧第二部分
79‧‧‧管線/密封氣體量
178‧‧‧管線
179‧‧‧管線
180‧‧‧附加部分/第二製程流/氮量
181‧‧‧氣態氧/管線
Claims (10)
- 一種在蒸餾塔系統中藉低溫分離空氣來可變提取壓縮氣體產品(72;73)之方法,該蒸餾塔系統具有高壓塔(21)及低壓塔(22),其中全部之所用空氣在主空氣壓縮機(2)中被壓縮至第一壓力,該第一壓力比該高壓塔(21)之操作壓力高至少4bar,在該主空氣壓縮機(2)中被壓縮之所用空氣(7)的第一分流(8,11,14)在主熱交換器(13)中冷卻至中間溫度並在第一空氣渦輪機(15)中膨脹做功,經膨脹做功之第一分流(16)的至少一第一部分被導入(40;18,19,20)該蒸餾塔系統,在該主空氣壓縮機(2)中被壓縮之所用空氣的第二分流(12,27,29,30)在特定言之由該第一渦輪機(15)驅動之第一增壓壓縮機(9)中被再壓縮至高於該第一壓力之第二壓力,在該主熱交換器(13)中冷卻,而後膨脹(31)並被導入該蒸餾塔系統,自該蒸餾塔系統液態提取第一產品流(69;75)並且將其增壓(71;76)至第一產品壓力,該第一產品流在該第一產品壓力下在該主熱交換器(13)中蒸發或假蒸發並被加熱,該經加熱之第一產品流(72;77)作為第一壓縮氣體產品(GOX IC;GAN IC)被提取,至少包含78mol%氮之第一製程流在多級壓縮機(57/59)中由入口壓力被壓縮至最後壓力,其中該多級壓縮機由氮產品壓縮機(57/59)構成,並且該第一製程流由來自該低壓塔之第一氣態氮氣流(55,56)構 成,至少包含78mol%氮之第二製程流(180)在該多級壓縮機(2;57/59)之第一級下游至少間歇性地與該第一製程流混合,其中該第二製程流(180)由來自該高壓塔(21)之第一氣態氮氣流(178,179)構成,在第一操作模式下提取第一壓縮氣體產品之第一量,在第二操作模式下提取第一壓縮氣體產品之第二量,該第二量小於該第一量,在該第一操作模式下在該多級壓縮機(2;57/59)中壓縮該第二製程流(65;180)之第一量,該第一量亦可為零,並且在該第二操作模式下在該多級壓縮機(2;57/59)中壓縮該第二製程流(65;180)之第二量,該第二量大於該第二製程流之第一量。
- 如請求項1之方法,其特徵在於,該第二製程流或該第四製程流在該氮產品壓縮機之中間級與該第一製程流或該第二製程流混合。
- 如請求項1至2中任一項之方法,其特徵在於,在該第二操作模式下自該低壓塔(22)之下部區域提取氧氣流(181),將該氧氣流與來自該低壓塔(22)之上部區域的氮富集流(61)混合並且在該主熱交換器(13)中加熱該混合物。
- 如請求項1至3中任一項之方法,其特徵在於,在該主空氣壓縮機(2)中被壓縮之所用空氣(7)的第三分流(36,37)在該主熱交換器(13)中冷卻至中間溫度並在第二空氣渦輪機(38)中膨脹做功,並且該經膨脹做功之第三分流(39)的至少一第一部分被導入(40)該蒸餾塔系統, 其中該第二空氣渦輪機之渦輪機入口壓力特定言之等於該第一壓力。
- 如請求項4之方法,其特徵在於,在該主空氣壓縮機(2)中被壓縮之所用空氣(7)的第二分流(12,27,29,30)於該第一增壓壓縮機(9)下游在該主熱交換器(13)中冷卻至中間溫度,在作為冷壓縮機運行且由該第二渦輪機(38)驅動之第二增壓壓縮機(28)中被再壓縮至高於該第一壓力之第三壓力,在該主熱交換器(13)中冷卻,而後膨脹(31)並被導入(32)該蒸餾塔系統。
- 如請求項1至5中任一項之方法,其特徵在於,在該主空氣壓縮機(2)中被壓縮之空氣(7)的第四分流(41,42)在該第一壓力下在該主熱交換器(13)中冷卻,而後膨脹(43)並被導入該蒸餾塔系統。
- 如請求項4或5或者如請求項6回溯引用請求項4或5中任一項之方法,其特徵在於,該第三分流(37,339)在該第二空氣渦輪機(38)中膨脹至一壓力,該壓力比該高壓塔(21)之操作壓力高至少1bar,並且經膨脹做功之第三分流(339)在該主熱交換器(13)中進一步冷卻,而後膨脹(341)並被導入該蒸餾塔系統。
- 如請求項1至7中任一項之方法,其特徵在於,在該第一操作模式下在該主空氣壓縮機(2)中壓縮所用空氣之第一量,並且在該第二操作模式下在該主空氣壓縮機(2)中壓縮所用空氣之第二量,其中所用空氣之該第二量與所用空氣之該第一量之比大於第一壓縮氣體產品之該第二量與第一壓縮氣體產品之該第一量之比, 特定言之大3%以上。
- 如請求項1至8中任一項之,方法,其特徵在於,在該主空氣壓縮機(2)中被壓縮之所用空氣(7)的第一分流(8,11)在被導入該主熱交換器(13)之前在由該第一渦輪機(15)驅動之熱運行的第一增壓壓縮機(9)中被再壓縮。
- 一種藉低溫分離空氣來可變提取壓縮氣體產品(72;73)之裝置,包括:蒸餾塔系統,其具有高壓塔(21)及低壓塔(22),主空氣壓縮機(2),用於將全部之所用空氣壓縮至第一壓力,該第一壓力比該高壓塔(21)之操作壓力高至少4bar,用於在主熱交換器(13)中將在該主空氣壓縮機(2)中被壓縮之所用空氣(7)的第一分流(8,11,14)冷卻至中間溫度的手段,第一空氣渦輪機(15),用於使該經冷卻之第一分流膨脹做功,用於將該經膨脹做功之第一分流(16)導入(40;18,19,20)該蒸餾塔系統之手段,第一增壓壓縮機(9),用於將在該主空氣壓縮機(2)中被壓縮之所用空氣的第二分流(12,27,29,30)再壓縮至高於該第一壓力之第二壓力,其中該增壓壓縮機(9)特定言之由該第一渦輪機(15)驅動,用於在該主熱交換器(13)中冷卻該經再壓縮之第二分流的手段,用於使該經冷卻之第二分流膨脹(31)並將其導入該蒸餾塔系統之手段,用於自該蒸餾塔系統液態提取第一產品流(69;75)並將該液態第一產品流增壓(71;76)至第一產品壓力之手段,用於在該主熱交換器(13)中在該第一產品壓力下蒸發或假蒸發 並加熱該第一產品流之手段,用於將該經加熱之第一產品流(72;77)作為第一壓縮氣體產品(GOX IC;GAN IC)加以提取之手段,多級壓縮機(57/59),用於將至少包含78mol%氮之第一製程流由入口壓力壓縮至最後壓力,其中該多級壓縮機由氮產品壓縮機(57/59)構成,並且該第一製程流由來自該低壓塔之第一氣態氮流(55,56)構成,用於使至少包含78mol%氮之第二製程流(180)在該多級壓縮機(57/59)之第一級下游與該第一製程流混合之手段,其中該第二製程流(180)由來自該高壓塔(21)之第一氣態氮流(178,179)構成,用於在第一與第二操作模式間切換之手段,其中在該第一操作模式下提取第一壓縮氣體產品之第一量,在該第二操作模式下提取第一壓縮氣體產品之第二量,該第二量小於該第一量,並且該等用於在該第一與該第二操作模式間切換之手段被構造成使得在該第一操作模式下在該多級壓縮機(57/59)中將該第二製程流(180)之第一量由入口壓力壓縮至最後壓力,該第一量亦可為零,並且在該第二操作模式下在該多級壓縮機(57/59)中壓縮該第二製程流(180)之第二量,該第二量大於該第二製程流之第一量。
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Families Citing this family (31)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2963367A1 (de) * | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch |
KR102446458B1 (ko) * | 2016-08-30 | 2022-09-23 | 8 리버스 캐피탈, 엘엘씨 | 고압의 산소를 생성하기 위한 극저온 공기 분리 방법 |
EP3312533A1 (de) | 2016-10-18 | 2018-04-25 | Linde Aktiengesellschaft | Verfahren zur luftzerlegung und luftzerlegungsanlage |
DE102017010001A1 (de) | 2016-11-04 | 2018-05-09 | Linde Aktiengesellschaft | Verfahren und Anlage zur Tieftemperaturzerlegung von Luft |
DE102016015292A1 (de) | 2016-12-22 | 2018-06-28 | Linde Aktiengesellschaft | Verfahren zur Bereitstellung eines oder mehrerer Luftprodukte mit einer Luftzerlegungsanlage |
EP3343158A1 (de) | 2016-12-28 | 2018-07-04 | Linde Aktiengesellschaft | Verfahren zur herstellung eines oder mehrerer luftprodukte und luftzerlegungsanlage |
US10359231B2 (en) | 2017-04-12 | 2019-07-23 | Praxair Technology, Inc. | Method for controlling production of high pressure gaseous oxygen in an air separation unit |
FR3066809B1 (fr) * | 2017-05-24 | 2020-01-31 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede et appareil pour la separation de l'air par distillation cryogenique |
WO2018219501A1 (de) | 2017-05-31 | 2018-12-06 | Linde Aktiengesellschaft | Verfahren zur gewinnung eines oder mehrerer luftprodukte und luftzerlegungsanlage |
EP3410050B1 (de) * | 2017-06-02 | 2019-05-01 | Linde Aktiengesellschaft | Verfahren zur gewinnung eines oder mehrerer luftprodukte und luftzerlegungsanlage |
FR3072451B1 (fr) * | 2017-10-13 | 2022-01-21 | Air Liquide | Procede et appareil de separation d'air par distillation cryogenique |
US11578916B2 (en) * | 2017-12-29 | 2023-02-14 | L'Air Liquide, Societe Anonyme Pour L'Etude Et L'Exploitation Des Procedes Georqes Claude | Method and device for producing air product based on cryogenic rectification |
WO2019214847A1 (de) | 2018-05-07 | 2019-11-14 | Linde Aktiengesellschaft | Verfahren zur gewinnung eines oder mehrerer luftprodukte und luftzerlegungsanlage |
EP3620739A1 (de) | 2018-09-05 | 2020-03-11 | Linde Aktiengesellschaft | Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage |
US20220026145A1 (en) | 2018-10-09 | 2022-01-27 | Linde Gmbh | Method for obtaining one or more air products and air separation system |
US20210381762A1 (en) | 2018-10-26 | 2021-12-09 | Linde Gmbh | Method for obtaining one or more air products, and air separation unit |
DE202018005045U1 (de) | 2018-10-31 | 2018-12-17 | Linde Aktiengesellschaft | Anlage zur Gewinnung von Argon durch Tieftemperaturzerlegung von Luft |
EP3671085A1 (de) | 2018-12-18 | 2020-06-24 | Linde GmbH | Anordnung und verfahren zum rückgewinnen von verdichtungswärme aus luft, die in einer luftbearbeitungsanlage verdichtet und bearbeitet wird |
DE102019000335A1 (de) | 2019-01-18 | 2020-07-23 | Linde Aktiengesellschaft | Verfahren zur Bereitstellung von Luftprodukten und Luftzerlegungsanlage |
EP3696486A1 (de) | 2019-02-13 | 2020-08-19 | Linde GmbH | Verfahren und anlage zur bereitstellung eines oder mehrerer sauerstoffreicher, gasförmiger luftprodukte |
EP3699534A1 (de) | 2019-02-19 | 2020-08-26 | Linde GmbH | Verfahren und luftzerlegungsanlage zur variablen bereitstellung eines gasförmigen, druckbeaufschlagten luftprodukts |
EP3699535A1 (de) | 2019-02-19 | 2020-08-26 | Linde GmbH | Verfahren und luftzerlegungsanlage zur variablen bereitstellung eines gasförmigen, druckbeaufschlagten luftprodukts |
EP4211409A1 (de) | 2020-09-08 | 2023-07-19 | Linde GmbH | Verfahren zur gewinnung eines oder mehrerer luftprodukte und luftzerlegungsanlage |
WO2022053173A1 (de) | 2020-09-08 | 2022-03-17 | Linde Gmbh | Verfahren und anlage zur tieftemperaturzerlegung von luft |
US20240003620A1 (en) | 2020-11-24 | 2024-01-04 | Linde Gmbh | Process and plant for cryogenic separation of air |
CN117501057A (zh) | 2021-06-17 | 2024-02-02 | 林德有限责任公司 | 一种用于提供加压富氧气态空气产物的方法和设备 |
DE202021002439U1 (de) | 2021-07-17 | 2021-10-20 | Linde Gmbh | Verdichter |
TW202326047A (zh) | 2021-09-02 | 2023-07-01 | 德商林德有限公司 | 獲取一種或數種空氣產物的方法及空氣分離設備 |
DE202021002895U1 (de) | 2021-09-07 | 2022-02-09 | Linde GmbH | Anlage zur Tieftemperaturzerlegung von Luft |
WO2023051946A1 (de) | 2021-09-29 | 2023-04-06 | Linde Gmbh | Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage |
CN114674112A (zh) * | 2022-04-07 | 2022-06-28 | 安阳钢铁股份有限公司 | 一种液化装置氧氮自动转换方法 |
Family Cites Families (87)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE830805C (de) | 1944-11-19 | 1952-02-07 | Linde Eismasch Ag | Verfahren zur Gas-, insbesondere zur Luftzerlegung |
US2712738A (en) | 1952-01-10 | 1955-07-12 | Linde S Eismaschinen Ag | Method for fractionating air by liquefaction and rectification |
DE901542C (de) | 1952-01-10 | 1954-01-11 | Linde Eismasch Ag | Verfahren zur Zerlegung von Luft durch Verfluessigung und Rektifikation |
US2784572A (en) | 1953-01-02 | 1957-03-12 | Linde S Eismaschinen Ag | Method for fractionating air by liquefaction and rectification |
DE952908C (de) | 1953-10-11 | 1956-11-22 | Linde Eismasch Ag | Verfahren zur Zerlegung von Luft |
DE1124529B (de) | 1957-07-04 | 1962-03-01 | Linde Eismasch Ag | Verfahren und Einrichtung zur Durchfuehrung von Waermeaustauschvorgaengen in einer mit vorgeschalteten Regeneratoren arbeitenden Gaszerlegungsanlage |
DE1103363B (de) | 1958-09-24 | 1961-03-30 | Linde Eismasch Ag | Verfahren und Vorrichtung zur Erzeugung eines ausgeglichenen Kaeltehaushaltes bei der Gewinnung von unter hoeherem Druck stehenden Gasgemischen und/oder Gasgemisch-komponenten durch Rektifikation |
DE1112997B (de) | 1960-08-13 | 1961-08-24 | Linde Eismasch Ag | Verfahren und Einrichtung zur Gaszerlegung durch Rektifikation bei tiefer Temperatur |
DE1117616B (de) | 1960-10-14 | 1961-11-23 | Linde Eismasch Ag | Verfahren und Einrichtung zum Gewinnen besonders reiner Zerlegungsprodukte in Tieftemperaturgaszerlegungsanlagen |
DE1226616B (de) | 1961-11-29 | 1966-10-13 | Linde Ag | Verfahren und Einrichtung zur Gewinnung von gasfoermigem Drucksauerstoff mit gleichzeitiger Erzeugung fluessiger Zerlegungsprodukte durch Tieftemperatur-Luftzerlegung |
DE1229561B (de) | 1962-12-21 | 1966-12-01 | Linde Ag | Verfahren und Vorrichtung zum Zerlegen von Luft durch Verfluessigung und Rektifikation mit Hilfe eines Inertgaskreislaufes |
DE1187248B (de) | 1963-03-29 | 1965-02-18 | Linde Eismasch Ag | Verfahren und Einrichtung zur Gewinnung von Sauerstoffgas mit 70 bis 98% O-Gehalt |
DE1199293B (de) | 1963-03-29 | 1965-08-26 | Linde Eismasch Ag | Verfahren und Vorrichtung zur Luftzerlegung in einem Einsaeulenrektifikator |
DE1258882B (de) | 1963-06-19 | 1968-01-18 | Linde Ag | Verfahren und Anlage zur Luftzerlegung durch Rektifikation unter Verwendung eines Hochdruckgas-Kaeltekreislaufes zur Druckverdampfung fluessigen Sauerstoffs |
DE1235347B (de) | 1964-05-13 | 1967-03-02 | Linde Ag | Verfahren und Vorrichtung zum Betrieb von umschaltbaren Waermeaustauschern bei der Tieftemperaturgaszerlegung |
DE1263037B (de) | 1965-05-19 | 1968-03-14 | Linde Ag | Verfahren zur Zerlegung von Luft in einer Rektifikationssaeule und damit gekoppelterZerlegung eines Wasserstoff enthaltenden Gasgemisches |
DE1501722A1 (de) | 1966-01-13 | 1969-06-26 | Linde Ag | Verfahren zur Tieftemperatur-Luftzerlegung zur Erzeugung von hochverdichtetem gasfoermigem und/oder fluessigem Sauerstoff |
DE1501723A1 (de) | 1966-01-13 | 1969-06-26 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung gasfoermigen Hochdrucksauerstoffs bei der Tieftemperaturrektifikation von Luft |
DE2535132C3 (de) | 1975-08-06 | 1981-08-20 | Linde Ag, 6200 Wiesbaden | Verfahren und Vorrichtung zur Herstellung von Drucksauerstoff durch zweistufige Tieftemperaturrektifikation von Luft |
SU787829A1 (ru) * | 1976-09-10 | 1980-12-15 | Предприятие П/Я А-3605 | Способ получени жидких и газообразных компонентов воздуха |
DE2646690A1 (de) | 1976-10-15 | 1978-04-20 | Linde Ag | Verfahren und vorrichtung zur herstellung einer mischung von sauerstoff und wasserdampf unter druck |
DE3367023D1 (en) | 1982-05-03 | 1986-11-20 | Linde Ag | Process and apparatus for obtaining gaseous oxygen at elevated pressure |
DE3738559A1 (de) * | 1987-11-13 | 1989-05-24 | Linde Ag | Verfahren zur luftzerlegung durch tieftemperaturrektifikation |
EP0383994A3 (de) | 1989-02-23 | 1990-11-07 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Luftzerlegung durch Rektifikation |
RU2054609C1 (ru) * | 1990-12-04 | 1996-02-20 | Балашихинское научно-производственное объединение криогенного машиностроения им.40-летия Октября "Криогенмаш" | Способ разделения воздуха |
DE4109945A1 (de) | 1991-03-26 | 1992-10-01 | Linde Ag | Verfahren zur tieftemperaturzerlegung von luft |
FR2689224B1 (fr) | 1992-03-24 | 1994-05-06 | Lair Liquide | Procede et installation de production d'azote sous haute pression et d'oxygene. |
FR2692664A1 (fr) * | 1992-06-23 | 1993-12-24 | Lair Liquide | Procédé et installation de production d'oxygène gazeux sous pression. |
DE4443190A1 (de) | 1994-12-05 | 1996-06-13 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
DE19526785C1 (de) | 1995-07-21 | 1997-02-20 | Linde Ag | Verfahren und Vorrichtung zur variablen Erzeugung eines gasförmigen Druckprodukts |
DE19529681C2 (de) | 1995-08-11 | 1997-05-28 | Linde Ag | Verfahren und Vorrichtung zur Luftzerlegung durch Tieftemperaturrektifikation |
US5678425A (en) * | 1996-06-07 | 1997-10-21 | Air Products And Chemicals, Inc. | Method and apparatus for producing liquid products from air in various proportions |
DE19732887A1 (de) | 1997-07-30 | 1999-02-04 | Linde Ag | Verfahren zur Luftzerlegung |
DE19803437A1 (de) | 1998-01-29 | 1999-03-18 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung eines Druckprodukts durch Tieftemperaturzerlegung von Luft |
DE19815885A1 (de) | 1998-04-08 | 1999-10-14 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt bei der Tieftemperaturzerlegung von Luft |
EP0955509B1 (de) | 1998-04-30 | 2004-12-22 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von hochreinem Sauerstoff |
EP1031804B1 (de) | 1999-02-26 | 2004-02-04 | Linde AG | Tieftemperaturzerlegung von Luft mit Stickstoff Rückführung |
DE19908451A1 (de) | 1999-02-26 | 2000-08-31 | Linde Tech Gase Gmbh | Zweisäulensystem zur Tieftemperaturzerlegung von Luft |
DE19909744A1 (de) | 1999-03-05 | 2000-05-04 | Linde Ag | Zweisäulensystem zur Tieftemperaturzerlegung von Luft |
US6116052A (en) * | 1999-04-09 | 2000-09-12 | Air Liquide Process And Construction | Cryogenic air separation process and installation |
DE59909750D1 (de) | 1999-07-05 | 2004-07-22 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
DE19936816A1 (de) | 1999-08-05 | 2001-02-08 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Sauerstoff unter überatmosphärischem Druck |
DE19954593B4 (de) | 1999-11-12 | 2008-04-10 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
DE10013073A1 (de) | 2000-03-17 | 2000-10-19 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
DE10013075A1 (de) | 2000-03-17 | 2001-09-20 | Linde Ag | Verfahren zur Gewinnung von gasförmigem und flüssigem Stickstoff mit variablem Anteil des Flüssigprodukts |
DE10015602A1 (de) | 2000-03-29 | 2001-10-04 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung eines Druckprodukts durch Tieftemperaturzerlegung von Luft |
DE10018200A1 (de) | 2000-04-12 | 2001-10-18 | Linde Gas Ag | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff durch Tieftemperaturzerlegung von Luft |
DE10021081A1 (de) | 2000-04-28 | 2002-01-03 | Linde Ag | Verfahren und Vorrichtung zum Wärmeaustausch |
DE10060678A1 (de) | 2000-12-06 | 2002-06-13 | Linde Ag | Maschinensystem zur arbeitsleistenden Entspannung zweier Prozess-Ströme |
DE10115258A1 (de) | 2001-03-28 | 2002-07-18 | Linde Ag | Maschinensystem und dessen Anwendung |
DE10139727A1 (de) | 2001-08-13 | 2003-02-27 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung eines Druckprodukts durch Tieftemperaturzerlegung von Luft |
DE10153252A1 (de) | 2001-10-31 | 2003-05-15 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung von Luft |
US7188492B2 (en) * | 2002-01-18 | 2007-03-13 | Linde Aktiengesellschaft | Plate heat exchanger |
FR2831249A1 (fr) * | 2002-01-21 | 2003-04-25 | Air Liquide | Procede et installation de separation d'air par distillation cryogenique |
DE10213212A1 (de) | 2002-03-25 | 2002-10-17 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung zweier Druckprodukte durch Tieftemperatur-Luftzerlegung |
DE10213211A1 (de) | 2002-03-25 | 2002-10-17 | Linde Ag | Verfahren zur Tieftemperatur-Luftzerlegung mit abgeschottetem Kreislaufsystem |
DE10217091A1 (de) | 2002-04-17 | 2003-11-06 | Linde Ag | Drei-Säulen-System zur Tieftemperatur-Luftzerlegung mit Argongewinnung |
DE10238282A1 (de) | 2002-08-21 | 2003-05-28 | Linde Ag | Verfahren zur Tieftemperatur-Zerlegung von Luft |
RU2005122894A (ru) | 2002-12-19 | 2006-01-20 | Каргес-Фолконбридж, Инк. (Us) | Способ жидкостной экстракции |
DE10302389A1 (de) | 2003-01-22 | 2003-06-18 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
DE10334560A1 (de) | 2003-05-28 | 2004-12-16 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung von Luft |
DE10334559A1 (de) | 2003-05-28 | 2004-12-16 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung von Luft |
DE10332863A1 (de) | 2003-07-18 | 2004-02-26 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Krypton und/oder Xenon durch Tieftemperaturzerlegung von Luft |
US6962062B2 (en) * | 2003-12-10 | 2005-11-08 | L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Proédés Georges Claude | Process and apparatus for the separation of air by cryogenic distillation |
EP1544559A1 (de) | 2003-12-20 | 2005-06-22 | Linde AG | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
US7228715B2 (en) * | 2003-12-23 | 2007-06-12 | L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude | Cryogenic air separation process and apparatus |
DE102005029274A1 (de) | 2004-08-17 | 2006-02-23 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperatur-Zerlegung von Luft |
EP1666824A1 (de) | 2004-12-03 | 2006-06-07 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von Argon durch Tieftemperaturzerlegung von Luft |
EP1666823A1 (de) | 2004-12-03 | 2006-06-07 | Linde Aktiengesellschaft | Vorrichtung zur Tieftemperaturzerlegung eines Gasgemisches, insbesondere von Luft |
DE102005028012A1 (de) | 2005-06-16 | 2006-09-14 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
WO2007033838A1 (de) | 2005-09-23 | 2007-03-29 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
DE102006012241A1 (de) | 2006-03-15 | 2007-09-20 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
EP1845323A1 (de) | 2006-04-13 | 2007-10-17 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Erzeugung eines Druckprodukts durch Tieftemperatur-Luftzerlegung |
DE102006032731A1 (de) | 2006-07-14 | 2007-01-18 | Linde Ag | Verfahren und Anlage zur Luftzerlegung |
EP1892490A1 (de) | 2006-08-16 | 2008-02-27 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur variablen Gewinnung eines Druckprodukts durch Tieftemperatur-Gaszerlegung |
US8020408B2 (en) * | 2006-12-06 | 2011-09-20 | Praxair Technology, Inc. | Separation method and apparatus |
DE102007014643A1 (de) | 2007-03-27 | 2007-09-20 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft |
DE102007031765A1 (de) | 2007-07-07 | 2009-01-08 | Linde Ag | Verfahren zur Tieftemperaturzerlegung von Luft |
DE102007031759A1 (de) | 2007-07-07 | 2009-01-08 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft |
EP2026024A1 (de) | 2007-07-30 | 2009-02-18 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von Argon durch Tieftemperaturzerlegung von Luft |
EP2235460B1 (de) | 2008-01-28 | 2018-06-20 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur tieftemperatur-luftzerlegung |
DE102008016355A1 (de) | 2008-03-29 | 2009-10-01 | Linde Ag | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
DE102010052545A1 (de) * | 2010-11-25 | 2012-05-31 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft |
EP2520886A1 (de) * | 2011-05-05 | 2012-11-07 | Linde AG | Verfahren und Vorrichtung zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft |
EP2600090B1 (de) * | 2011-12-01 | 2014-07-16 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Erzeugung von Drucksauerstoff durch Tieftemperaturzerlegung von Luft |
FR2995393B1 (fr) * | 2012-09-12 | 2014-10-03 | Air Liquide | Procede et appareil de separation d'air par distillation cryogenique. |
EP2963367A1 (de) * | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch |
-
2014
- 2014-07-05 EP EP14002307.8A patent/EP2963367A1/de not_active Withdrawn
-
2015
- 2015-06-25 EP EP15733625.6A patent/EP3164653A1/de not_active Withdrawn
- 2015-06-25 EP EP15735849.0A patent/EP3164654B1/de active Active
- 2015-06-25 RU RU2017103099A patent/RU2691210C2/ru active
- 2015-06-25 US US15/322,740 patent/US10215489B2/en not_active Expired - Fee Related
- 2015-06-25 WO PCT/EP2015/001285 patent/WO2016005031A1/de active Application Filing
- 2015-06-25 WO PCT/EP2015/001284 patent/WO2016005030A1/de active Application Filing
- 2015-06-25 US US15/322,468 patent/US10458702B2/en active Active
- 2015-06-25 CN CN201580036802.0A patent/CN106489059B/zh not_active Expired - Fee Related
- 2015-06-25 CN CN201580036844.4A patent/CN106662394B/zh active Active
- 2015-06-25 RU RU2017103309A patent/RU2690550C2/ru active
- 2015-07-03 TW TW104121752A patent/TW201607599A/zh unknown
- 2015-07-03 TW TW104121751A patent/TW201607598A/zh unknown
Also Published As
Publication number | Publication date |
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CN106489059A (zh) | 2017-03-08 |
US10458702B2 (en) | 2019-10-29 |
EP3164654A1 (de) | 2017-05-10 |
CN106489059B (zh) | 2019-11-05 |
RU2017103309A (ru) | 2018-08-06 |
CN106662394B (zh) | 2019-11-05 |
EP3164654B1 (de) | 2020-07-29 |
RU2017103309A3 (zh) | 2018-12-18 |
RU2017103099A3 (zh) | 2018-12-20 |
RU2691210C2 (ru) | 2019-06-11 |
US20170131028A1 (en) | 2017-05-11 |
TW201607599A (zh) | 2016-03-01 |
US20170153058A1 (en) | 2017-06-01 |
RU2017103099A (ru) | 2018-08-06 |
CN106662394A (zh) | 2017-05-10 |
WO2016005030A1 (de) | 2016-01-14 |
RU2690550C2 (ru) | 2019-06-04 |
EP2963367A1 (de) | 2016-01-06 |
EP3164653A1 (de) | 2017-05-10 |
US10215489B2 (en) | 2019-02-26 |
WO2016005031A1 (de) | 2016-01-14 |
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