TW201718066A - 空氣分餾設備、操作方法及控制裝置 - Google Patents

空氣分餾設備、操作方法及控制裝置 Download PDF

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TW201718066A
TW201718066A TW105123780A TW105123780A TW201718066A TW 201718066 A TW201718066 A TW 201718066A TW 105123780 A TW105123780 A TW 105123780A TW 105123780 A TW105123780 A TW 105123780A TW 201718066 A TW201718066 A TW 201718066A
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air
cooling
cooling water
recooling
temperature
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史蒂芬 朵依
柏哈德 普林格
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林德股份公司
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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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    • F25J3/04642—Recovering noble gases from air
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    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
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    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
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  • Thermal Sciences (AREA)
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Abstract

本發明係關於空氣分餾設備(100)，其中提供具有再冷卻裝置(11)之冷卻水迴路(10)用於冷卻壓縮空氣，其中該再冷卻裝置(11)經構形用於使用冷卻空氣來冷卻冷卻水。該再冷卻裝置(11)經構形以便至少在大於289K之冷卻空氣之濕球溫度下將該冷卻水冷卻至高於該濕球溫度不超過3K之溫度。本發明亦提供相應操作方法及控制裝置。

Description

空氣分餾設備、操作方法及控制裝置
根據獨立申請專利範圍之各別前言，本發明係關於空氣分餾設備、操作空氣分餾設備之方法及用於此一空氣分餾設備之控制裝置。
藉由在空氣分餾設備中低溫分餾空氣來產生呈液態或氣態之空氣產品係已知的，且闡述於(例如)H.-W.Häring(編輯)，Industrial Gases Processing,Wiley-VCH,2006，具體而言第2.2.5節「Cryogenic Rectification」中。本發明適用於相應空氣分餾設備之各個實施例。
空氣分餾設備具有可(例如)構形為雙柱系統、特定而言為經典林德(Linde)雙柱系統以及為三柱或多柱系統之蒸餾柱系統。除了用於分離呈液態及/或氣態之氮及/或氧(例如液態氧LOX、氣態氧GOX、液態氮LIN及/或氣態氮GAN)之蒸餾柱(即用於氮-氧分離之蒸餾柱)以外，可提供用於分離空氣之其他組份、特定而言稀有氣體氪、氙及/或氬之蒸餾柱。
空氣分餾設備之蒸餾柱系統係在其蒸餾柱中於不同操作壓力下操作。已知之雙柱系統具有(例如)(高)壓柱及低壓柱。高壓柱之操作壓力係(例如)4.3巴(bar)至6.9巴、特定而言約5.5巴。低壓柱係在(例如)1.2巴至1.7巴、特定而言約1.4巴之操作壓力下操作。本文中所指示之壓力係相應蒸餾柱之底部之絕對壓力。所指示之壓力在下文中將 亦稱為「蒸餾壓力」，此乃因在蒸餾柱內之各別進給空氣之分餾係在該等壓力下發生。此不排除能夠在蒸餾柱系統中之不同位置佔優之其他壓力。
將藉助各種空氣壓縮機或各種空氣壓縮機之組合(例如主空氣壓縮機及後壓縮機)達到壓力之冷卻壓縮空氣(進料空氣)進給至蒸餾柱系統中。所有空氣壓縮機可係多級的。由於空氣分餾設備中約95%之能量消耗來自上文所提及之空氣壓縮機，因此在此處存在最大之節省潛力。業內在根本上需要用於低溫分餾空氣之能量上更有效之製程及設備。
鑒於此背景，本發明提供空氣分餾設備、操作空氣分餾設備之方法及用於此一空氣分餾設備之控制裝置，其具有獨立申請專利範圍之各別特徵。本發明之實施例闡述於從屬申請專利範圍及下文之說明中。
通常，已在空氣分餾設備之空氣壓縮機中達到壓力之進料空氣在不同構形之冷卻裝置中再冷卻，以去除在壓縮期間產生之壓縮熱。該等冷卻裝置包含(例如)在一或多個壓縮級之間及下游之中間冷卻器及後冷卻器，如本身已知。將於空氣分餾設備之主空氣壓縮機中壓縮之空氣再冷卻可尤其(例如)在使用來自冷卻水迴路之冷卻水操作之直接接觸冷卻器中實現。另外，可提供可同樣使用冷卻水操作之間接熱交換器。在已知製程中，隨後在主熱交換器中使進料空氣達到極低溫度，即顯著低於0℃之溫度。
特定而言，為了降低空氣壓縮機之功率消耗之目的，實施再冷卻。此處冷卻水溫度愈低，製程空氣可愈進一步冷卻，此使得空氣壓縮機之功率消耗更低。另外，製程空氣因此在較低溫度下進入空氣分餾之實際製程中，包括進入主熱交換器中。因此，欲在主熱交換器中傳遞之熱量較低，由此此熱交換器可設計為具有較小體積且，另外， 必須藉由減壓產生較少之冷量。產生冷至(例如)120K至200K之適當低溫導致相當大之能量損失，其顯著大於在接近於環境溫度下實施之藉助冷卻水冷卻之情形。另外，必須製造得更大的低溫組件(熱交換器、渦輪機、閥)成本更高。
空氣分餾設備之冷卻水迴路通常包含再冷卻裝置，其中冷卻水迴路之升溫之冷卻水藉由藉助冷卻空氣之蒸發冷卻來冷卻。特定而言，已知類型之冷卻塔(亦如下文所解釋)可用作再冷卻裝置。相應空氣分餾設備揭示於(例如)EP 0 644 390 A1及JP 5 885093 A1中。本文中所使用之冷卻空氣通常來源於空氣分餾設備之周圍環境，且因此具有周圍環境依賴性之溫度、周圍環境依賴性之壓力及周圍環境依賴性之濕度。濕球溫度可自該三個參數測定。
濕球溫度係冷卻極限溫度之量度，即冷卻水可藉由在相應再冷卻裝置中直接蒸發冷卻理論上獲得之最低溫度。已知在潮濕表面釋放水與周圍大氣之吸水能力處於平衡狀態。由於藉由蒸發所產生之冷量，冷卻極限溫度低於隨相對大氣濕度而變之空氣溫度。在蒸發冷卻期間溫度降低愈大，周圍空氣愈乾燥。濕球溫度與在相應再冷卻裝置中實際獲得之經冷卻之冷卻水之間之溫度差在此項技術中稱為冷卻極限差。再冷卻裝置(例如冷卻塔)之性能係藉由填料之比表面積、液體對氣體之比率及壓力降確定。為獲得小的冷卻極限差，如由於上文所提及之較低冷卻水溫度之優點而原則上所期望，使得用於安裝再冷卻裝置之資本成本顯著較大。
因此，所用之冷卻極限差係藉由包括所提及態樣之經濟考慮來確定。在先前關於工業設備中強制通風再冷卻裝置之出版物中，3K至5K之冷卻極限差通常指示為經濟上可行的，參見(例如)Z.K.Morvay及D.D.Gvozdenac,「Applied Industrial Energy and Environmental Management,Part III：Toolbox-Fundamentals for Analysis and Calculation of Energy and Environmental Performance,Toolbox 12：Cooling Towers」,Chichester,Wiley,2008。然而，此數字通常在未指示相應環境條件及由此產生之濕球溫度之情形下給出。冷卻極限差顯著低於3K之再冷卻裝置亦可在技術上達成，但通常視此為不經濟的。相應地，較低冷卻極限差通常僅在實驗室規模上使用，如同(例如)根據V.D.Papaefthimiou等人之出版物「Thermodynamic Study of Wet Cooling Tower Performance」,Int.J.Energ.Res.30(6),2006,411-426之情形。
關於再冷卻裝置及其設計之其他細節，可參考相關專業文獻(例如)H.-D.Held、H.-G.Schnell、Kühlwasser：Verfahren der Systeme der Aufbereitung und Kühlung von Süßwasser,Brackwasser-und Meerwasser zur industriellen Kühlung，第5版，Vulkan,2000；H.Rietschel、K.Fitzner、Raumklimatechnik，第2卷：Raumluft und Raumkühltechnik，第16版，Springer,2008；J.J.McKetta，Encyclopedia of Chemical Processing and Design，第58卷，Marcel Dekker,1997；P.N.Ananthanarayanan，Basic Refrigeration and Air Conditioning，第3版，Tata McGraw-Hill,2006；及B.Buecker，Power Plant Water Chemistry：A Practical Guide,PennWell,1997。特定而言，可強調藉助再冷卻裝置可達成之冷卻極限差可由熟習此項技術者基於已知計算方法可靠地預測。因此，下文據稱，再冷卻裝置經構形使得其將冷卻水冷卻至高於濕球溫度最大溫度值之溫度，且此對於熟習此項技術者建議制定再冷卻裝置之尺寸，使得其具有上文所提及之性質，即具有相應冷卻極限差。特定而言，熟習此項技術者在此將以適當方式計及或提供填料之比表面積、液體對氣體之比率及壓力降。
本發明之優點
令人驚訝地且與在強制通風再冷卻裝置(參見(例如)上文引用之 出版物Z.K.Morvay及D.D.Gvozdenac)之主題方面之佔優觀點相反，根據本發明已認識到，基於總的操作成本(總擁有成本(Total Cost of Ownership，TCO))，低於3K之冷卻極限差為許多空氣分餾設備提供經濟優勢。此處，在設計條件下，在給定濕球溫度下，冷卻極限差應隨資本價值(以貨幣單位每kW、淨現值(Net Present Value，NPV)表示)變化來選擇。因此，具有相同資本價值之設備可獲得與各別環境條件無關地去除相同特定熱量之再冷卻裝置。此使得可系統性選擇隨資本價值變化之冷卻塔。如所提及，根據佔優觀點，特定而言對於實際工業應用(例如空氣分餾設備)而言，顯著高於3K之冷卻極限差被視為適當的。已被數次引用之Z.K.Morvay及D.D.Gvozdenac之出版物提出一系列之效率改良但未提出降低冷卻極限差。
因此，本發明提出空氣分餾設備，其中提供具有再冷卻裝置之冷卻水迴路用於冷卻壓縮空氣，其中再冷卻裝置經構形用於使用冷卻空氣來冷卻冷卻水。本發明之空氣分餾設備之特徵在於再冷卻裝置經構形用於至少在大於289K之冷卻空氣之濕球溫度下將冷卻水冷卻至高於濕球溫度不超過3K之溫度。換言之，在指定條件下，藉助本發明之空氣分餾設備之再冷卻裝置達成3K或更小、特定而言2K或更小或1K或更小之冷卻極限差。
如在本發明之上下文中已發現，在文獻中經常發現之冷卻極限差小於2K之再冷卻裝置在技術上不可行之聲明係錯誤的。同樣地，已發現僅3K至5K之冷卻極限差在經濟上可行之通常概況係不正確的。如在本發明之上下文中已認識到，具有固定冷卻極限差而忽略濕球溫度之再冷卻裝置之可行性及經濟實用性之指示不具預測價值。
如根據本發明已認識到及下文所記載，冷卻極限差降低至低於3K之值使得在大於289K之中等及高濕球溫度下空氣分餾設備之經濟性得以顯著改良。因此，本發明係基於對關於一般空氣分餾製程及低 溫製程之冷卻塔設計之知識說明之重要新的評估。
在本發明之上下文中，已能夠顯示，有效操作將冷卻水再冷卻至極其接近熱力學上可能之最小值(即濕球溫度)之再冷卻裝置容許空氣分餾設備中顯著之能量節省。此在圖2及3中清楚地示出，並解釋其他細節。有效操作且因此通常較大之再冷卻裝置之額外資本成本(CAPEX)在平均約一年中藉由節省運行成本(OPEX)來攤銷。較大之再冷卻裝置之短的攤銷時間係由於其在空氣分餾設備之總成本中佔較小比例(通常約2%)所致。表1給出習用再冷卻裝置及根據本發明之再冷卻裝置(本文中為相應冷卻塔)之資本成本及操作成本之概述。
在經濟評價中，舉例而言，可查看與根據圖2及3之根據本發明設計之再冷卻裝置相比習用設計之再冷卻裝置。假定具有用於容納回流之水箱之(強制通風)冷卻塔為再冷卻裝置。較低之冷卻極限溫度導致具有同樣增大之箱之較大之再冷卻裝置及因此更高之資本成本。在兩種情形下水之質量流量相同。決定性之事實係，在大型冷卻塔之情形下，對於相同量之冷卻水，更大量之空氣可流過再冷卻裝置；此空氣吸收蒸發水並同時使得更大之對流冷卻成為可能。此降低根據本發明之冷卻塔中之冷卻水溫度且，由於空氣壓縮機及能量最佳化之冷卻塔之較低之功率消耗，使得操作成本較低。在所考慮之情形下，假定在每一情形下電力成本為0.07€/kWh。使用500,000標準立方米製程空氣/小時之空氣分餾設備之再冷卻裝置之結果報告於表1中，操作成本涉及一年。
出於本發明之目的，有利地使用再冷卻裝置，該再冷卻裝置以使得其將冷卻水冷卻至高於濕球溫度至少0.5K之溫度、例如亦至少1K、至少1.5K或至少2K之方式經構形。自以上考慮可推導出最小及最大冷卻極限差之最佳值範圍。
根據本發明之空氣分餾設備原則上可具有具任何構形之再冷卻裝置，但此尤佳包含冷卻塔。經證明特別是具有強制通風之再冷卻裝置或冷卻塔經常用於空氣分餾設備中，且其具有低的維護需求。如上所解釋，冷卻塔特定而言容許藉由增大來相對簡單地降低冷卻極限溫度。
如上文所提及，已使用再冷卻裝置進行冷卻之冷卻水尤其適於相應空氣分餾設備中之壓縮機下游之後冷卻，使得根據本發明之空氣分餾設備之冷卻水迴路有利地包含位於空氣壓縮機或相應空氣壓縮機之級之下游之熱交換器。出於本發明之目的，「空氣壓縮機」係單級或多級配置，其經構形用於增加壓力，特定而言徑向壓縮機或渦輪壓縮機。一或多個熱交換器可存在於一或多個壓縮機級之下游。
在本發明之上下文中，再冷卻裝置之冷卻區範圍可係特定而言5K至25K、特定而言8K至12K、通常約10K。
本發明進一步延伸至操作空氣分餾設備之方法，其中提供具有再冷卻裝置之冷卻水迴路用於冷卻壓縮空氣，其中再冷卻裝置經構形用於使用冷卻空氣來冷卻冷卻水。本發明之方法之特徵在於再冷卻裝置係以至少在大於289K之冷卻空氣之濕球溫度下其將冷卻水冷卻至 高於濕球溫度不超過3K之溫度之方式操作。同樣地，本發明延伸至空氣分餾設備之控制裝置，其經構形用於實施此類型之方法。在兩種情形下，可參考上文關於特徵及優點所述之內容。
1‧‧‧壓縮機級
2‧‧‧壓縮機級
3‧‧‧中間冷卻器
10‧‧‧冷卻水迴路
11‧‧‧再冷卻裝置
100‧‧‧空氣分餾設備
101‧‧‧過濾器
102‧‧‧主空氣壓縮機、壓縮機
103‧‧‧直接接觸冷卻器、熱交換器
104‧‧‧蒸發冷卻器
105‧‧‧吸附器組
106‧‧‧電操作及/或蒸汽操作之再生氣體加熱器件、再生氣體加熱器
107‧‧‧後壓縮機、壓縮機
108‧‧‧主熱交換器
110‧‧‧蒸餾柱系統
111‧‧‧高壓柱
112‧‧‧低壓柱
113‧‧‧氬富集柱
114‧‧‧純氬柱
201‧‧‧數據點
202‧‧‧數據點
203‧‧‧數據點
a‧‧‧進料空氣流、經壓縮及冷卻之進料空氣流
b‧‧‧冷卻水流、水流
c‧‧‧流、水流
d‧‧‧水流
e‧‧‧水流
f‧‧‧空氣流、流
g‧‧‧水流
h‧‧‧經壓縮及冷卻之進料空氣流
i‧‧‧再生氣體流
k‧‧‧流
l‧‧‧壓縮空氣流
m‧‧‧子流、流
n‧‧‧子流、流
o‧‧‧氣態氮流
p‧‧‧流
q‧‧‧流
r‧‧‧液體富氧流
s‧‧‧流
圖1以示意性製程流程圖之形式顯示根據本發明之實施例之空氣分餾設備。
圖2繪製冷卻水溫度及相應濕球溫度來圖解說明本發明之實施例。
圖3A及3B顯示根據本發明可實現之冷卻水之額外冷卻及相關聯之能量節省。
下面將參考顯示本發明之較佳實施例之附圖來圖解說明本發明。
在圖1中，根據本發明之尤佳實施例之空氣分餾設備係以示意性製程流程圖之形式顯示且整體上命名為100。
進料空氣流a經由過濾器101進給至空氣分餾設備100中、藉助主空氣壓縮機102壓縮並在直接接觸冷卻器103中進行冷卻，直接接觸冷卻器103尤其供應有來自蒸發冷卻器104之冷卻水流b。水流b藉助未單獨指示之幫浦引入至直接接觸冷卻器103中。為提供冷卻水流b，向蒸發冷卻器104供應流c之水，流c之水亦可部分地進給至直接接觸冷卻器103中，而不用在蒸發冷卻器104中進行預先冷卻。自直接接觸冷卻器103取出水流d。
所示之水流b、c及d亦及直接接觸冷卻器103及蒸發冷卻器104整合至冷卻水迴路(本文中表示為10)中，冷卻水迴路亦可包含未示出之任何其他水流、幫浦、直接及間接熱交換器等。舉例而言，如本文中以大為簡化之形式顯示，主空氣壓縮機102可具有至少兩個壓縮機級1 及2，在該兩個壓縮機之間藉助中間冷卻器3進行中間冷卻。空氣分餾設備之典型主空氣壓縮機102包含5至9個壓縮機級及相應數量之中間冷卻器。呈流s之形式之冷卻水可進給至所圖解說明之中間冷卻器3中，該中間冷卻器3經構形用於間接熱交換。流s特定而言可係流c之子流，即同樣地在冷卻水迴路10中循環之冷卻水。類似的情況適用於如下文所解釋之其他(後)冷卻器。舉例而言，為了補償蒸發損失，其他水流可在任何地方進給至冷卻水迴路10中，如本文中指示為水流e。此外，水流、調節器件、量測感測器及諸如此類之間之交叉連接可佈置於冷卻水迴路10中之有利位置。
冷卻水迴路10之核心組件係再冷卻裝置11，在本文中再冷卻裝置11顯示為濕式冷卻器且可構形為(例如)具有強制通風之冷卻塔。然而，如上文所提及，任何其他實施例亦係可能的。再冷卻裝置11經構形用於根據上文所提及之本發明實施例操作。具有在空氣分餾設備100之位置處佔優之濕球溫度之大氣空氣之流f進給至再冷卻裝置11中。再冷卻裝置11(例如)經構形用於將待冷卻之水流g(在所繪示之實例中由水流d及e形成)之水冷卻至高於空氣流f之濕球溫度不超過3K之溫度位準。此在空氣流f之濕球溫度高於289K時尤其適用。
經壓縮及冷卻之進料空氣流a(現命名為h)之進一步處理在很大程度上對應於習用空氣分餾設備中者，例如如在H.-W.Häring(編輯)，Industrial Gases Processing,Wiley-VCH,2006，具體而言第2.2.5節「Cryogenic Rectification」中所闡述之空氣分餾設備中者。
經壓縮及冷卻之進料空氣流h進給至包含交替操作之吸附器容器之吸附器組105，且可藉助再生氣體流i再生。再生氣體流i可藉助電操作及/或蒸汽操作之再生氣體加熱器件106來加熱。為提供再生氣體流i，可使用流k，流k之提供將在下文中更加詳細地闡述。
已於吸附器組50中乾燥之壓縮空氣流係表示為1。端視空氣分餾 設備100之構形，壓縮空氣流l可在使得後壓縮必需或非必需(後者係在高空氣壓力製程之情形下)之壓力下提供。在所示實例中，壓縮空氣流l之子流m進給至後壓縮機107。後壓縮機107之未單獨指定之後冷卻器可同樣地使用來自冷卻水迴路10之水進行冷卻。
根據所繪示之實施例，壓縮空氣流l之子流m及未經後壓縮之子流n進給至主熱交換器108並在不同溫度位準下自此取出。流m可藉助發電機渦輪109減壓，且在與流n合併之後進給至蒸餾柱系統110之高壓柱111中。壓縮空氣流l之其他子流可以有利的方式形成、冷卻、後壓縮、減壓及同樣地進給至蒸餾柱系統110之柱中，例如本文中未示出之已知節流流。
高壓柱111以及低壓柱112一起形成已知類型之雙塔系統。在所示之實例中，蒸餾柱系統額外包含氬富集柱113及純氬柱114，但該等不需要提供。可提供其他蒸餾柱。
蒸餾柱系統110之操作已知且因此將不予解釋。在所示之實例中，蒸餾柱系統110尤其供應有氣態氮流o(呈流p之形式之「不純氮」)，自其流k及/或流q可在主熱交換器108中加熱之後形成且可進給至再生氣體加熱器106或蒸發冷卻器104，且可取出液體富氧流r。亦可使用(例如)冷的富氮流代替流q。其他流將不詳細解釋。任何流可在主熱交換器108中加熱、在主熱交換器108之上游或下游壓縮或加壓、與其他流合併並分為子流。
圖2顯示1年中各月份之平均冷卻水溫度及相應濕球溫度以圖解說明本發明之實施例。冷卻水溫度(以K表示)係繪製在縱座標上，相對於繪製在橫座標上之濕球溫度(以K表示)。在圖中，濕球溫度係以數據點201之形式顯示，在構形為冷卻塔之再冷卻裝置之習用設計中之冷卻水溫度係以數據點202之形式顯示，且在根據本發明之實施例之設計中之冷卻水溫度係以數據點203之形式顯示。
習用設計造成289K之濕球溫度之8K之冷卻極限差。根據所繪示之本發明之實施例，冷卻極限差降低5克耳文(kelvin)至3K。使用更有效之冷卻塔及因此降低冷卻極限溫度導致兩個效應，即首先更冷之冷卻水及其次冷卻水溫度與濕球溫度之間之更小之相對差。此意味著對於具有相對較小冷卻極限差之設計而言，在相對較冷的月份中，冷卻塔之效率損失基本上較低。在較冷月份中大型冷卻塔之較低效率損失之原因在於可偏向於空氣移動之水/空氣比率。對於兩種冷卻塔變化形式而言，水之質量流量相同，且關鍵因素係在大型冷卻塔之情形下，對於相同量之冷卻水，更大量之空氣可流過再冷卻裝置，且此空氣吸收蒸發水並同時容許大的對流冷卻。此效應尤其在空氣可吸收極少水之低空氣溫度下產生積極貢獻。
圖3A及3B顯示根據本發明可實現之冷卻水之額外冷卻(圖3A)及相關聯之能量節省(圖3B)。在圖3A中溫度差(以K表示)及在圖3B中能量差(以kW表示)係繪製在縱座標上，相對於繪製在橫座標上之月份(一月(J)至十二月(D))。
如自圖3A可見，實質上平均獲得5K冷卻器冷卻水。在圖3B中相應可見之能量節省係270kW至450kW/月，且導致每年平均節省340kW。340kW之壓縮機功率消耗減少對應於總壓縮機功率消耗之1.5%。
1‧‧‧壓縮機級
2‧‧‧壓縮機級
3‧‧‧中間冷卻器
10‧‧‧冷卻水迴路
11‧‧‧再冷卻裝置
100‧‧‧空氣分餾設備
101‧‧‧過濾器
102‧‧‧主空氣壓縮機、壓縮機
103‧‧‧直接接觸冷卻器、熱交換器
104‧‧‧蒸發冷卻器
105‧‧‧吸附器組
106‧‧‧電操作及/或蒸汽操作之再生氣體加熱器件、再生氣體加熱器
107‧‧‧後壓縮機、壓縮機
108‧‧‧主熱交換器
110‧‧‧蒸餾柱系統
111‧‧‧高壓柱
112‧‧‧低壓柱
113‧‧‧氬富集柱
114‧‧‧純氬柱
a‧‧‧進料空氣流、經壓縮及冷卻之進料空氣流
b‧‧‧冷卻水流、水流
c‧‧‧流、水流
d‧‧‧水流
e‧‧‧水流
f‧‧‧空氣流、流
g‧‧‧水流
h‧‧‧經壓縮及冷卻之進料空氣流
i‧‧‧再生氣體流
k‧‧‧流
l‧‧‧壓縮空氣流
m‧‧‧子流、流
n‧‧‧子流、流
o‧‧‧氣態氮流
p‧‧‧流
q‧‧‧流
r‧‧‧液體富氧流
s‧‧‧流

Claims (8)

  1. 一種空氣分餾設備(100)，其中提供具有再冷卻裝置(11)之冷卻水迴路(10)用於冷卻壓縮空氣，其中該再冷卻裝置(11)經構形用於使用冷卻空氣來冷卻冷卻水，其特徵在於該再冷卻裝置(11)經構形以便至少在大於289K之該冷卻空氣之濕球溫度下將該冷卻水冷卻至高於該濕球溫度不超過3K之溫度。
  2. 如請求項1之空氣分餾設備(100)，其中該再冷卻裝置(11)經構形以便將該冷卻水冷卻至高於該濕球溫度至少0.5K之溫度。
  3. 如請求項1或2之空氣分餾設備(100)，其中該再冷卻裝置(11)包含冷卻塔。
  4. 如請求項3之空氣分餾設備(100)，其中該再冷卻裝置(11)具有強制通風。
  5. 如前述請求項中任一項之空氣分餾設備(100)，其中該冷卻水迴路(10)包含熱交換器(103)，該熱交換器(103)係佈置在壓縮機(102、107)之下游。
  6. 如前述請求項中任一項之空氣分餾設備(100)，其中提供5K至25K之冷卻區範圍。
  7. 一種操作空氣分餾設備(100)之方法，其中提供具有再冷卻裝置(11)之冷卻水迴路(10)用於冷卻壓縮空氣，其中該再冷卻裝置(11)經構形用於使用冷卻空氣來冷卻冷卻水，其特徵在於該再冷卻裝置(11)經構形並操作以便至少在大於289K之該冷卻空氣之濕球溫度下將該冷卻水冷卻至高於該濕球溫度不超過3K之溫度。
  8. 如請求項7之方法，其中該再冷卻裝置(11)中之填料之比表面積及/或液體對氣體之比率及/或壓力降係以使得至少在大於289K 之該冷卻空氣之濕球溫度下將該冷卻水冷卻至高於該濕球溫度不超過3K之溫度之方式經選擇及/或設置。
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