TWI712770B - 在空氣分離廠中獲取空氣產品之方法及空氣分離廠 - Google Patents

在空氣分離廠中獲取空氣產品之方法及空氣分離廠 Download PDF

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TWI712770B
TWI712770B TW106101115A TW106101115A TWI712770B TW I712770 B TWI712770 B TW I712770B TW 106101115 A TW106101115 A TW 106101115A TW 106101115 A TW106101115 A TW 106101115A TW I712770 B TWI712770 B TW I712770B
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tank
cryogenic liquid
liquid
air
during
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TW106101115A
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TW201730493A (zh
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史戴芬 羅克納
勞夫 史波林
克里斯汀 基默曼
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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
    • F25J3/04763—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
    • F25J3/04848—Control strategy, e.g. advanced process control or dynamic modeling
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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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
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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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    • F25J3/04—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
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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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    • F25J3/0409—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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    • 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
    • F25J3/04096—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 argon or argon enriched stream
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    • F25J3/04163—Hot end purification of the feed air
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Abstract

本發明提供使用空氣分離廠(100)獲取空氣產品(GOX-IC)之方法，該空氣分離廠(100)具有蒸餾塔系統(12, 38)及具有第一槽(71)及第二槽(72)之槽系統(70)，其中低溫液體(41)係自該蒸餾塔系統(12, 38)中抽出。提出使用具有額外第三槽(73)之槽系統(70)作為該槽系統(70)，且其中抽出的該低溫液體(41)至少部分未加熱地轉移至該第三槽(73)，其中用於提供該空氣產品(GOX-IC)之該低溫液體係以液態自該第三槽(73)抽出，汽化或轉化至超臨界狀態，且自該空氣分離廠(100)排出，及/或其中用於提供該空氣產品(GOX-IC)之該低溫液體係以液態自該第三槽(73)抽出且以液態儲存在第四槽(76)中。本發明亦係關於空氣分離廠(100)。

Description

在空氣分離廠中獲取空氣產品之方法及空氣分離廠
本發明係關於在空氣分離廠中獲取空氣產品之方法及經設計用於實施該方法之空氣分離廠。
已知藉由在空氣分離廠中低溫分離空氣來生產液體或氣態形式之空氣產品且闡述於(例如) H.-W. Häring (編輯), Industrial Gases Processing, Wiley-VCH, 2006, 尤其章節2.2.5, 「Cryogenic Rectification」中。 很多工業用途需要壓縮氧，且為了生產壓縮氧，可使用具有稱為內部壓縮之空氣分離廠。此類型之空氣分離廠亦在(例如)Häring中闡述且參考其中之圖2.3A進行闡釋。在該等分離廠中，以低溫液體狀態加壓之低溫液體、尤其液態氧，抵靠熱傳遞介質汽化，並最終作為加壓氣體產品排出。與隨後壓縮已經以氣體形式存在之產品相比，內部壓縮尤其具有能量優點。 在該情況下，在超臨界壓力下無真正相變；而係使低溫液體自液態變為超臨界狀態。術語「偽汽化」或「去液化」亦用於此情況下。自液態變為超臨界狀態之低溫液體使處於高壓下之熱傳遞介質液化(或視情形，若熱傳遞介質處於超臨界壓力下，則使其「偽液化」)。熱傳遞介質通常係由供應至空氣分離廠之空氣之一部分形成。 若適當，本闡釋亦可用於其他空氣產品，例如氮或氬，其亦可藉由使用內部壓縮以氣態或超臨界狀態獲取，且先前作為低溫液體存在。 為在空氣分離廠中增加空氣產品之壓力，已知使用稱為加壓壓縮者，其(例如)闡述於DE 676 616C及EP 0 464 630 A1中。如(例如)在US 6 295 840 B1中所揭示，空氣產品亦可儲存於槽系統中，且在此處藉助經壓縮進料空氣之分流來加壓。 需要提高在空氣分離廠中、尤其在具有所討論之槽系統之空氣分離廠中產生相應空氣產品之可能性。
針對此背景，本發明提出在空氣分離廠中獲取空氣產品之方法及經設置用於實施該方法之空氣分離廠，其具有獨立申請專利範圍之特徵。較佳構形形成附屬申請專利範圍及以下闡述之標的物。 本申請案使用術語「壓力位準」及「溫度位準」以表徵壓力及溫度，該等術語意欲表示，為實現本發明概念，相應廠中之壓力及溫度無需以精確的壓力或溫度值之形式使用。然而，該等壓力及溫度通常在圍繞中心值之某些範圍內移動，例如±1%、5%、10%、20%或甚至50%。在該情況下，相應壓力位準及溫度位準可在不相交範圍中或在重疊範圍中。特定而言，例如，壓力位準包括(例如)由於冷卻效應或管道損失造成之不可避免的或預期的壓力損失。此亦適用於溫度位準。此處以巴(bar)指示之壓力位準係絕對壓力。
本發明之優點 本發明提出使用具有蒸餾塔系統及具有第一槽及第二槽之槽系統之空氣分離廠獲取空氣產品之方法。 在本發明方法之情況中，低溫液體(例如純氧或前文所提及之其他空氣產品中之一者)係自蒸餾塔系統中抽出且至少部分以液體形式儲存於槽系統中。在自槽系統抽出之後，低溫液體可用作空氣產品。在本發明情況中，然後使用具有第一及第二槽之槽系統，交替地向該等第一及第二槽供應低溫液體。換言之，在第一時段期間，將低溫液體供應至第一槽而非第二槽，且在第二時段期間供應至第二槽而非第一槽。交替操作進一步涉及，在第一時段期間自第二槽而非第一槽抽出低溫液體，且在第二時段期間自第一槽而非第二槽抽出低溫液體。亦可提供使用兩個以上經受相應循環之槽。然而，該等槽仍包含第一及第二槽及分別在第一或第二時段中之相應供應或抽出。 使用相應槽系統使得可在內部壓縮方法中製備具有指定純度之產品，此乃因該方法允許使用不能連續實施之分析方法。在其中使用幫浦進行加壓之習用內部壓縮方法中，此係不可能的，此乃因在此情況下，幫浦排出流連續地且直接地供應至加熱。在本發明方法之情況中，例如可在第一時段之後驗證儲存在第一槽中之低溫液體之純度，且在第二時段之後對儲存在第二槽中之液體進行相同純度驗證。若此純度對應於設定點值，則該低溫液體係作為空氣產品提供。若純度不匹配設定點值，則可丟棄相應低溫液體或可有利地將其返回至蒸餾塔系統中。 然而，尤其當在槽之間切換時，即在第一時段與第二時段之間或在第二時段與第一時段之間切換時，或若(例如)由於令人不滿意之純度導致槽內容物不能作為空氣產品提供，此類型之交替操作導致自槽系統提供低溫液體之中斷，其最終轉化為空氣產品之不連續生產。此可給連接至相應空氣分離廠之消費者帶來問題，其供應令人不滿意，且亦在可能用於加熱低溫液體之器件(例如空氣分離廠之主熱交換器)中導致有問題的影響。 因此，本發明提出使用具有額外第三槽之槽系統作為槽系統，其中將在第一時段期間自第二槽及在第二時段期間自第一槽抽出之低溫液體至少部分(且尤其至少暫時地)未加熱轉移至第三槽中。在此情況下，亦可提出僅將在第一時段期間自第二槽及在第二時段期間自第一槽抽出之低溫液體之一部分未加熱轉移至第三槽中，及如下所闡釋經由旁路直接提供低溫液體之另一部分作為空氣產品或以另一種形式使用。在該情況下，第三槽用作接收器或緩衝儲存器，其填充有足以橋接上文所闡釋之時段之適量的低溫液體。 若在第一時段期間自第二槽及在第二時段期間自第一槽中抽出之低溫液體係以抽出溫度位準自第二或第一槽轉移至第三槽中，則至第三槽中之轉移係「未加熱的」。若低溫液體未經歷主動升溫措施或未加熱，則情形如此。因此，具體而言，該低溫液體未藉助任何用於加熱之熱交換器、加熱器、逆流單元等進給。如上文已關於術語「溫度位準」所述，此不排除不可避免之熱輸入可導致一定、但非主動進行之加熱。術語「溫度位準」將此考慮在內，使得在所述情況中，所提及之抽出溫度位準仍可低於進入第三槽中之進給溫度位準。特定而言，未加熱轉移至第三槽中以避免汽化損失。 因此，根據本發明，儲存在第一或第二槽中之低溫液體不再(或不僅)自其中移除並用作空氣產品。而係至少部分係藉由使用未加熱轉移至第三槽中之低溫液體或其一部分來提供空氣產品。然而，在本發明情況中，如所提及，亦可提供允許自第一或第二槽移除之旁路管線，使得空氣產品亦可部分使用儲存在其中，而非轉移至第三槽中之低溫液體提供。此使得(例如)若第三槽完全充滿且已建立令人滿意之純度，則亦可自第一或第二槽直接抽出。此外，可提出並非所有未加熱轉移至第三槽中之低溫液體皆用於提供空氣產品。未加熱轉移至第三槽中之低溫液體之一部分可以液態自第三槽中抽出，另有他用。例如，已在各別槽中汽化之低溫液體之部分亦可能不用於提供空氣產品。 亦根據本發明提出，用於提供空氣產品之來自第三槽之低溫液體係以液態自第三槽抽出，汽化或自液體轉化為超臨界狀態，且自空氣分離廠排出，及/或用於提供空氣產品之低溫液體係以液態自第三槽抽出且以液態儲存在第四槽中。 第四槽可係具有第一至第三槽之槽系統之一部分，但其亦可單獨(例如作為另一個槽系統之一部分)提供。第四槽可位於空氣分離廠內，例如在冷箱內，或在亦包圍第一至第三槽之隔熱外殼內。然而，亦可將第四槽佈置在空氣分離廠之外部。因此，在本發明情況中，空氣產品可係處於氣態或處於超臨界狀態之空氣產品，及/或液體空氣產品。正如液體空氣產品一般，氣態空氣產品亦可儲存在空氣分離廠內或廠外，尤其在適當氣體槽中。 有利地，將低溫液體在操作下文亦稱為「第二分離塔」之蒸餾塔系統之相應塔、尤其純氧塔之壓力位準下自空氣分離廠之蒸餾塔系統抽出。將低溫液體以本文中稱為「第一」壓力位準之壓力位準供應至槽系統之第一槽及第二槽。若在分離塔與第一或第二槽之間未佈置影響壓力之器件(例如幫浦)，則第一壓力位準可對應於自蒸餾塔系統抽出低溫液體之壓力位準。若(例如)使用相應幫浦，則第一壓力位準亦可高於分離塔之壓力位準。將低溫液體以第二較高壓力位準(儲存壓力)供應至槽系統之第三槽，該第二較高壓力位準可尤其基於欲提供空氣產品之壓力(產品壓力)來測定。儲存壓力有利地略高於產品壓力，使得可在無額外幫浦或壓縮機下排出。第二壓力位準可尤其藉由在第一及/或第二槽中實施加壓汽化來達成。 藉由使用所揭示槽系統及壓力增加，本發明組合習用內部壓縮方法之優點(即連續生產空氣產品)及經改良分析可能性之優點。此經改良之分析可能性使得可在任何時刻確保且記錄空氣產品之高純度。 若欲生產氣態或超臨界空氣產品，則在自第三槽(或經由上文所提及旁路管線自第一及第二槽)抽出低溫液體之後，如所提及，此液體可尤其汽化或自液態轉化為超臨界狀態。汽化或轉化為超臨界狀態(為簡單起見，術語「汽化」在下文中將用於兩種情形)可在所使用之空氣分離廠內(例如)使用此廠之主熱交換器進行。對於空氣分離廠不可用之情形，亦可使用具有緊急供應汽化器之備用系統，該緊急供應汽化器不自空氣分離廠抽取汽化熱。然而，且如亦已提及，在自第三槽(或經由上文所提及旁路管線自第一及第二槽)抽出之後，低溫液體亦可以液體形式自空氣分離廠排出，以液體形式(例如)在槽中運輸至消費者，並在消費者處以液體或(汽化後)氣態使用。
較佳地，第一壓力位準，即將低溫液體供應至第一及第二槽之壓力位準為約1.3巴至7巴。端視需要，第二壓力位準係在2巴與100巴之間，但高於第一壓力位準。在本發明情況中，考慮到消費者之壓力需求，可進行尤其在時間方面靈活之壓力增加。
根據本發明之一實施例，可在進給至第一槽中及第二槽中之前使用幫浦使低溫液體達到第一壓力位準。在此實施例中，本發明組合使用相應幫浦之習用內部壓縮方法(但其由於壓力連續增加而使得不可能實施不連續分析方法)與其中交替供應不同槽之方法之優點。
使用具有兩個槽之槽系統實施之習用方法涉及加壓汽化。在加壓汽化中，由於壓力增加需要相應低溫液體之一部分，故產品損失不可避免。此產品損失可高達10%。使用幫浦減少該產品損失。此處亦不可避免之槽中之閃蒸損失為約5%，且因此顯著低於由於加壓汽化導致之損失。即使相應幫浦需要額外能量，較高產品產率亦較此可能的額外能量需求更重要。
然後本發明在對個別空氣產品(例如氧)具有極高純度要求之空氣分離廠中提供特定優點。在該等極高純度要求之情形下，習用快速(常規)分析方法可接近檢測極限且必須使用更靈敏之分析方法(例如氣相層析)。然而，該等更靈敏分析方法需要較習用方法更多之時間來測定量測值，且因此需要實施不連續量測。
此外，本發明方法與僅在消費者處進行相應空氣產品(例如氧)之汽化之方法相比節省能量。總之，可節省約1kW/Nm3/h之能量。
容量受最大運輸尺寸限制之小型空氣分離廠尤其關注與本發明相關之優點。效率改良導致產率相應增加。
儘管如前文所提及藉助幫浦提高低溫液體之壓力在某些情形下可係有利的，但本發明原則上亦可用於在具有純加壓汽化之相應槽系統中獲得相當之優點。此使得可完全省去幫浦，其使得可更具成本效益地構建相應空氣分離廠。在加壓汽化中省去移動或驅動部件尤其允許節能及低維護操作。若無論如何欲提供氣態或超臨界空氣產品，則在加壓汽化之情形中產生之汽化損失無關緊要。亦可將藉助幫浦之壓力增加與額外加壓汽化組合。 如已提及，本發明方法尤其適合於提供高純度空氣產品，此乃因可在加熱並排出至設備邊界之前實施不連續分析。換言之，在本發明情況中，有利地測定在第一時段期間供應至第一槽且在第二時段期間供應至第二槽之低溫液體之純度。對於相應分析，可使用已建立之純度測試方法，例如光譜方法及/或氣相層析。 在本發明情況中，然後僅在低溫液體之純度對應於設定點值時，有利地將該低溫液體在第一時段期間自第二槽轉移至第三槽，且在第二時段期間自第一槽轉移至第三槽。因此，第三槽始終填充有限定純度之低溫液體，且可在任何時間用於提供空氣產品而無需額外分析。 若低溫液體之純度匹配設定點值，但其可有利地在第一時段期間自第二槽且在第二時段期間自第一槽返回至蒸餾塔系統。尤其在該方法變化形式中，使用第三槽使得本發明尤其有利，此乃因相應中斷可藉由自第三槽抽出低溫液體來平衡。因此有利地提出，第三槽保持一定量之低溫液體，該低溫液體之量至少與可儲存在第一槽及/或第二槽中之低溫液體之量一樣大，或至少大到足以橋接切換時間(在此期間，不可自前兩個容器抽出液體)，以允許連續抽出。此使得即使由於純度與設定點值不對應而導致完全充滿之第一或第二槽之內容物必須返回至蒸餾塔系統或被丟棄，仍可連續加熱低溫液體並將該低溫液體作為空氣產品排出。 特定而言，本發明適用於生產純氧之空氣分離廠中。在此類型之空氣分離廠中，蒸餾塔系統具有第一分離塔及第二分離塔。第一分離塔用於產生流體流，該流體流經富集至第一氧含量且其在第二分離塔中用於產生純液態氧，該純液態氧可至少部分自第二分離塔抽出作為低溫液體。藉由使用第三槽，本發明允許連續提供高純度氧。 特定而言，本發明可與如在(例如) US 2009/107177 A1中所闡述之申請人之SPECTRA方法結合使用。然而，本發明並不限於此。此類型之方法涉及使用第一分離塔以進一步產生經富集至第二氧含量之流體流及經富集至第三氧含量之流體流。將經富集至第二氧含量之流體流有利地在經富集至第一氧含量之流體流下方自第一分離塔排出。因此其具有較高氧含量。經富集至第三氧含量之流體流有利地自第一分離塔之儲槽中抽出。然後尤其在第一分離塔之冷凝器中及在主熱交換器中將該兩種流體流加熱至不同溫度，其中經富集至第二氧含量之經加熱流體流在耦合至膨脹機之壓縮機中至少部分經壓縮，冷卻並返回至第一分離塔。相比之下，經富集至第三氧含量之流體流之一部分用於驅動膨脹機。對於相應方法之其他細節，參考附圖1。證明相應方法在能量上尤其有利。 有利地，為加熱隨後作為空氣產品提供之低溫液體，使用空氣分離廠之主熱交換器。此外或其另一選擇為，然而亦可使用特殊汽化器。若空氣分離廠之主熱交換器容量不足，及/或若欲提供額外量之空氣產品(例如相應熱交換器能夠提供(若暫時地))，則尤其可使用相應汽化器。 本發明擴展到經設計用於獲取空氣產品之空氣分離廠。空氣分離廠包含蒸餾塔系統及具有第一槽及第二槽之槽系統且具有在如相應器件申請專利範圍中所指示之特徵。 有利地，相應空氣分離廠經設計用於實施如上文所詳細闡釋之方法。因此，在此點上明確地參考相應特徵及優點。 下文參考圖解說明本發明之較佳實施例之附圖更詳細地闡釋本發明。 圖式詳細說明 在以下附圖中，相互對應元件係用相同參考符號指示，且為清楚起見，將不重複闡釋。在該情況下，圖2及圖3分別顯示如可整合到根據圖1之空氣分離廠中或不同設計之空氣分離廠中之槽系統。在該情況下，槽系統之整合係由亦指示於圖1中之元件給出。 圖1以廠示意圖之形式示意性顯示本發明之一實施例之空氣分離廠。空氣分離廠作為整體具有標籤100。 藉由空氣壓縮機3經由過濾器2吸入大氣空氣1 (AIR)，在空氣壓縮機3中將其壓縮至6巴與20巴之間、較佳約9巴之絕對壓力。在流動穿過後冷卻器4及用於分離水(H2O)之水分離器5之後，在純化裝置7中淨化壓縮空氣6，該純化裝置7具有一對填充有吸附材料、較佳分子篩之容器。將純化空氣8在主熱交換器9中冷卻至接近露點，並部分液化。將冷卻空氣10之第一部分11經由節流閥51引入第一分離塔12中。注射較佳在儲槽上方若干個實際或理論塔板處進行。 單塔12之操作壓力(頂部)係在6巴與20巴之間、較佳約9巴。其頂部冷凝器13係用流體流18及流體流14冷卻。流體流18係自空氣注射點上方若干個實際或理論塔板處或與空氣注射點高度相同之中間點抽離，且流體流14係自第一分離塔12之儲槽抽離。在上文闡釋之情況中，已將流體流18標記為「經富集至第二氧含量之流體流」，且已將流體流14標記為「經富集至第三氧含量之流體流」。 在第一分離塔12之頂部抽離氣態氮15、16作為第一分離塔12之主要產品，在主熱交換器9中經加熱至約環境溫度，且最終經由管線17抽離作為加壓氣體產品(PGAN)。藉助頂部冷凝器13進給其他氣態氮。在頂部冷凝器13中獲取之冷凝物52之一部分53可作為液氮產品(PLIN)獲取；剩餘部分54作為回流輸送到第一分離塔12之頂部。 流體流14係在頂部冷凝器13中在2巴與9巴之間、較佳約4巴之壓力下汽化，且以氣態形式經由管線19流動到主熱交換器9之冷端。將其在中間溫度下以流20之形式自主熱交換器9之冷端抽出，且在膨脹機21中膨脹至高於大氣壓力約300毫巴以進行工作，該膨脹機21在所示實例中採用透平膨脹機之形式。氣態不純淨氧產品(GOX-Imp.)經由管線60離開主熱交換器9。膨脹機21機械耦合至(冷)壓縮機30及在所示實例中採用油壓制動器形式之制動器件22。將膨脹流體流23在主熱交換器9中加熱至約環境溫度。將熱流體流24作為流體流25排放到大氣(ATM)及/或可能在加熱器件28中加熱之後用作再生氣體26、27。 流體流18係在頂部冷凝器13中在2巴與9巴之間、較佳約4巴之壓力下汽化，且以氣態形式經由管線29流動到壓縮機30，在此其經再壓縮到接近第一分離塔12之操作壓力。將再壓縮流體流31在主熱交換器9中冷卻回到塔溫度且最終經由管線32進給回到第一分離塔12之儲槽。如所闡述之流體流14及18之處理對應於已提及之SPECTRA方法。 將基本上不含重質揮發性污染物之先前標記為「經富集至第一氧含量之流體流」之流體流36以液態自第一分離塔12之中間點抽離，該點佈置於空氣注射點上方5至25個理論或實際塔板處。若適當，將流體流36在經設計作為純氧塔之第二分離塔38之儲槽汽化器37中再冷卻，且然後經由管線39及節流閥40輸送到純氧塔38之頂部。純氧塔38之操作壓力(頂部)係在1.3巴與4巴之間、較佳約2.5巴。 第二分離塔38之儲槽汽化器37亦使用冷卻進料空氣10之第二部分42來操作。然後進料空氣流42至少部分、例如全部冷凝且經由管線43流動到第一分離塔12，其中其係大致在剩餘進料空氣11之注射高度處經引入，或引入塔儲槽中。 將純氧作為低溫液體41自第二分離塔38之儲槽抽出，視情況藉助幫浦55升高至2巴與100巴之間、較佳約12巴之升高壓力，且引入至在隨後的圖2及圖3中所示之槽佈置70中。在槽佈置70中之中間儲存之後，將低溫液體經由管線56進給到主熱交換器9之冷端，在此其在升高壓力下汽化且加熱到約環境溫度，且最終經由管線57作為氣態產品(GOX-IC)獲取。 將第二分離塔38之頂部氣體58混合到先前提及之膨脹第二流體流23中(參照連接A)。若相關，則將進料空氣之一部分經由旁路管線59引導到冷壓縮機30之入口以防止後者之浪湧(稱為防浪湧控制)。 必要時，可在幫浦55之上游及/或下游自空氣分離廠100抽出作為液體部分之液態氧(在圖式中標記為LOX)。此外，可在主熱交換器9中在與進料空氣之間接熱交換(圖式中未顯示)中汽化亦來自液體槽之外部液體(例如液氬、液氮或液態氧)。 圖2以廠示意圖之形式顯示本發明之一實施例之槽系統，其可用於如圖1所圖解說明之空氣分離廠100中，且作為整體具有標籤70。 已參考圖1闡釋之幫浦55用於使流體流41之低溫液體自第一壓力位準達到第二壓力位準。第一壓力位準可尤其對應於可操作如圖1所示之空氣分離廠100之第二分離塔38 (純氧塔)之壓力位準。第二壓力位準係(例如) 2巴至100巴。 將加壓流體流41供應到第一槽71或第二槽72。如多次闡釋，相對於彼此交替地向槽71及72供應流體流41之低溫液體，即在第一時段期間，將流體流41之低溫液體供應到第一槽71，而非第二槽72，且在第二時段期間供應到第二槽72，而非第一槽71。例如，可提供槽控制器80用於控制用於此目的之閥71a及72a。 如亦多次闡釋，始終自槽71、72抽出低溫液體，在該抽出時刻不向該等槽供應流體流41之低溫液體。將此液體未加熱轉移到第三槽73中。如已闡釋，例如在第三槽73完全充滿之情況下，且如此處所說明，亦可提出藉助管線74直接推動相應流體並將其供應至加熱。如亦提及，流體之加熱可在(例如)相應空氣分離廠(例如圖1之空氣分離廠100)之主熱交換器9中及/或在額外汽化器90中進行。 圖3以廠示意圖之形式圖解說明本發明之另一實施例之槽系統。圖3之槽系統亦標記為70。圖3中所圖解說明之槽系統70裝備有加壓汽化器件75。此處視情況提供幫浦55，如在圖2之槽系統70中及/或在圖1之空氣分離廠100中。在加壓汽化之情況下，通常省略相應幫浦55且將流41之低溫液體在對應於「第一壓力位準」之純氧塔38中之蒸餾壓力下分別注射到槽71或72中。加壓汽化器件75汽化以液體形式分別自液槽71或72抽出之流41之低溫液體之一部分。將經汽化及加壓之氣體分別進給到槽71或72之頂部空間。因此可省去幫浦55，且可僅使用加壓汽化。 如此處所顯示，用於提供液體空氣產品之低溫液體係以液態自第三槽73抽出，並在主熱交換器9中及/或額外汽化器90中汽化，或自液體轉化為超臨界狀態並自空氣分離廠排出。然而，用於提供液體空氣產品之低溫液體亦可以液態自第三槽73抽出，並以液體形式儲存在第四槽76中，直到使用其為止。已闡釋細節。第三槽73上游及/或下游之其他抽出點亦係可能的。
1‧‧‧大氣空氣 2‧‧‧過濾器 3‧‧‧空氣壓縮機 4‧‧‧後冷卻器 5‧‧‧水分離器 6‧‧‧壓縮空氣 7‧‧‧純化裝置 8‧‧‧純化空氣 9‧‧‧主熱交換器 10‧‧‧冷卻空氣/冷卻進料空氣 11‧‧‧第一部分/剩餘進料空氣 12‧‧‧第一分離塔/單塔/蒸餾塔系統 13‧‧‧頂部冷凝器 14‧‧‧流體流/經加熱流體流 15‧‧‧氣態氮 16‧‧‧氣態氮 17‧‧‧管線 18‧‧‧流體流 19‧‧‧管線 20‧‧‧流 21‧‧‧膨脹機 22‧‧‧制動器件 23‧‧‧膨脹流體流/第二流體流 24‧‧‧熱流體流 25‧‧‧流體流 26‧‧‧再生氣體 27‧‧‧再生氣體 28‧‧‧加熱器件 29‧‧‧管線 30‧‧‧(冷)壓縮機/壓縮機 31‧‧‧再壓縮流體流 32‧‧‧管線 36‧‧‧流體流 37‧‧‧儲槽汽化器 38‧‧‧第二分離塔/純氧塔/蒸餾塔系統 39‧‧‧管線 40‧‧‧節流閥 41‧‧‧低溫液體/流體流/加壓流體流/流 42‧‧‧第二部分/進料空氣流 43‧‧‧管線 51‧‧‧節流閥 52‧‧‧冷凝物 53‧‧‧部分 54‧‧‧剩餘部分 55‧‧‧幫浦 56‧‧‧管線 57‧‧‧管線 58‧‧‧頂部氣體 59‧‧‧旁路管線 60‧‧‧管線 70‧‧‧槽佈置/槽系統 71‧‧‧第一槽/槽 71a‧‧‧閥 72‧‧‧第二槽/槽 72a‧‧‧閥 73‧‧‧第三槽/額外第三槽 74‧‧‧管線 75‧‧‧加壓汽化器件 76‧‧‧第四槽 80‧‧‧槽控制器/汽化器 90‧‧‧額外汽化器 100‧‧‧空氣分離廠
圖1以廠示意圖之形式顯示本發明之一實施例之空氣分離廠。 圖2以廠示意圖之形式顯示本發明之一實施例之槽系統。 圖3以廠示意圖之形式顯示本發明之一實施例之槽系統。
1‧‧‧大氣空氣
2‧‧‧過濾器
3‧‧‧空氣壓縮機
4‧‧‧後冷卻器
5‧‧‧水分離器
6‧‧‧壓縮空氣
7‧‧‧純化裝置
8‧‧‧純化空氣
9‧‧‧主熱交換器
10‧‧‧冷卻空氣/冷卻進料空氣
11‧‧‧第一部分/剩餘進料空氣
12‧‧‧第一分離塔/單塔/蒸餾塔系統
13‧‧‧頂部冷凝器
14‧‧‧流體流/經加熱流體流
15‧‧‧氣態氮
16‧‧‧氣態氮
17‧‧‧管線
18‧‧‧流體流
19‧‧‧管線
20‧‧‧流
21‧‧‧膨脹機
22‧‧‧制動器件
23‧‧‧膨脹流體流/第二流體流
24‧‧‧熱流體流
25‧‧‧流體流
26‧‧‧再生氣體
27‧‧‧再生氣體
28‧‧‧加熱器件
29‧‧‧管線
30‧‧‧(冷)壓縮機/壓縮機
31‧‧‧再壓縮流體流
32‧‧‧管線
36‧‧‧流體流
37‧‧‧儲槽汽化器
38‧‧‧第二分離塔/純氧塔/蒸餾塔系統
39‧‧‧管線
40‧‧‧節流閥
41‧‧‧低溫液體/流體流/加壓流體流/流
42‧‧‧第二部分/進料空氣流
43‧‧‧管線
51‧‧‧節流閥
52‧‧‧冷凝物
53‧‧‧部分
54‧‧‧剩餘部分
55‧‧‧幫浦
56‧‧‧管線
57‧‧‧管線
58‧‧‧頂部氣體
59‧‧‧旁路管線
60‧‧‧管線
70‧‧‧槽佈置/槽系統
100‧‧‧空氣分離廠

Claims (14)

  1. 一種使用空氣分離廠(100)獲取空氣產品(GOX-IC)的方法，該空氣分離廠(100)具有蒸餾塔系統(12,38)及具有第一槽(71)及第二槽(72)之槽系統(70)，其中低溫液體(41)係自該蒸餾塔系統(12,38)中抽出，至少部分儲存於該槽系統(70)中，且然後至少部分用作該空氣產品(GOX-IC)，其中在第一時段期間，將該低溫液體(41)供應至該第一槽(71)而非該第二槽(72)，且在第二時段期間供應至該第二槽(72)而非該第一槽(71)，且在該第一時段期間自該第二槽(72)而非該第一槽(71)抽出，且在該第二時段期間自該第一槽(71)而非該第二槽(72)抽出，該方法之特徵在於：該槽系統(70)包含額外第三槽(73)，且在於在該第一時段期間自該第二槽(72)抽出且在該第二時段期間自該第一槽(71)抽出的該低溫液體(41)至少部分未加熱地轉移至該第三槽(73)，且在於該空氣產品至少部分藉由使用未加熱轉移至該第三槽(73)中之該低溫液體或其一部分來提供，其中用於提供該空氣產品(GOX-IC)之來自該第三槽(73)之該低溫液體係以液態自該第三槽(73)抽出，汽化或自該液體轉化為超臨界狀態，且自該空氣分離廠(100)排出，及/或用於提供該空氣產品(GOX-IC)之來自該第三槽(73)之該低溫液體係以液態自該第三槽(73)抽出且以液態儲存在第四槽(76)中。
  2. 如請求項1之方法，其中以第一壓力位準將該低溫液體(41)供應至該第一槽(71)及該第二槽(72)，及/或其中以第二壓力位準將該低溫液體(41)儲存在該第三槽(73)中，該第二壓力位準係高於該第一壓力位準。
  3. 如請求項2之方法，其中該第一壓力位準係在1.3巴與7巴之間，且該第二壓力位準係在2巴與100巴之間。
  4. 如請求項2之方法，其中在引入該第一槽(71)及該第二槽(72)中之前將該低溫液體(41)以液態並使用幫浦(55)自該第一壓力位準升高到該第二壓力位準。
  5. 如請求項2之方法，其中該低溫液體(41)在該第一槽(71)及該第二槽(72)中經歷加壓汽化至該第二壓力位準。
  6. 如請求項1至5中任一項之方法，其中在該第一時段期間供應至該第一槽(71)且在該第二時段期間供應至該第二槽(72)之該低溫液體(41)之純度係在各別槽(71,72)中測定。
  7. 如請求項6之方法，其中僅在其純度對應於設定點值時，將該低溫液體(41)在該第一時段期間自該第二槽(72)轉移至該第三槽(73)，且在該第二時段期間自該第一槽(71)轉移至該第三槽(73)。
  8. 如請求項7之方法，其中若該低溫液體(41)之純度未對應於該設定點值，則將該流體在該第一時段期間自該第二槽且在該第二時段期間自該第一槽(71)返回至該蒸餾塔系統(12,38)。
  9. 如請求項1至5中任一項之方法，其中該第三槽(73)保持一定量之該 低溫液體(41)，該低溫液體之量至少與可儲存在該第一槽(71)及/或該第二槽(72)中之該低溫液體(41)之量一樣大。
  10. 如請求項1至5中任一項之方法，其中該蒸餾塔系統(12,38)包含第一分離塔(12)及第二分離塔(38)，該第一分離塔(12)用於產生流體流(36)，該流體流(36)經富集至第一氧含量且其在該第二分離塔(38)中用於產生純液態氧，該純液態氧自該第二分離塔(38)抽出，至少部分作為該低溫液體(41)。
  11. 如請求項10之方法，其中進一步使用該第一分離塔(12)以產生經富集至第二氧含量之流體流(18)及經富集至第三氧含量之流體流(14)，且將該等流體流加熱至不同溫度，其中經富集至該第二氧含量之該經加熱流體流(14)在耦合至膨脹機(21)之壓縮機(30)中至少部分經壓縮，冷卻並返回至該第一分離塔(12)，且經富集至該第三氧含量之該經加熱流體流(14)之一部分用於驅動該膨脹機(21)。
  12. 如請求項1至5中任一項之方法，其中該空氣分離廠(100)之主熱交換器(9)及/或汽化器(80)用於加熱該低溫液體(41)。
  13. 一種經設計用於獲取空氣產品(GOX-IC)之空氣分離廠(100)，其具有蒸餾塔系統(12,38)及具有第一槽(71)及第二槽(72)之槽系統(70)，經設計自該蒸餾塔系統(12,38)抽出低溫液體(41)，以將此液體之至少一部分儲存於該槽系統(70)中，且然後使用此液體之至少一部分作為該空氣產品 (GOX-IC)之構件，及經設計以在第一時段期間將該低溫液體(41)供應至該第一槽(71)而非該第二槽(72)，且在第二時段期間供應至該第二槽(72)而非該第一槽(71)，且在該第一時段期間將該液體自該第二槽(72)而非該第一槽(71)抽出，且在該第二時段期間自該第一槽(71)而非該第二槽(72)抽出之構件，該空氣分離廠(100)之特徵在於該槽系統(70)包含額外第三槽(73)，且在於提供構件，該等構件經設計以將在該第一時段期間自該第二槽(72)抽出且在該第二時段期間自該第一槽(71)抽出的該低溫液體(41)至少暫時地且至少部分未加熱地轉移至該第三槽(73)，且至少部分藉由使用未加熱轉移至該第三槽(73)中之該低溫液體或其一部分提供該空氣產品(GOX-IC)，其中提供構件，該等構件經設計以自該第三槽(73)抽出呈液態之用於提供該空氣產品(GOX-IC)之來自該第三槽(73)之該低溫液體，將此低溫液體汽化或自該液體轉化為超臨界狀態，且將其自該空氣分離廠(100)排出，及/或該等構件經設計以自該第三槽(73)抽出呈液態之用於提供該空氣產品(GOX-IC)之來自該第三槽(73)之該低溫液體，且將其以液態儲存在第四槽(76)中。
  14. 如請求項13之空氣分離廠(100)，其經設計用於實施如請求項1至12中任一項之方法。
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