TW202117249A - 空氣的低溫分離方法與設備 - Google Patents
空氣的低溫分離方法與設備 Download PDFInfo
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- TW202117249A TW202117249A TW109136634A TW109136634A TW202117249A TW 202117249 A TW202117249 A TW 202117249A TW 109136634 A TW109136634 A TW 109136634A TW 109136634 A TW109136634 A TW 109136634A TW 202117249 A TW202117249 A TW 202117249A
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- 238000000926 separation method Methods 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 44
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims abstract description 137
- 239000007788 liquid Substances 0.000 claims abstract description 83
- 229910052786 argon Inorganic materials 0.000 claims abstract description 69
- 239000007789 gas Substances 0.000 claims abstract description 63
- 238000001704 evaporation Methods 0.000 claims abstract description 35
- 230000008020 evaporation Effects 0.000 claims abstract description 26
- 239000000463 material Substances 0.000 claims description 48
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 35
- 239000001301 oxygen Substances 0.000 claims description 35
- 229910052760 oxygen Inorganic materials 0.000 claims description 35
- 238000005191 phase separation Methods 0.000 claims description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 54
- 229910052757 nitrogen Inorganic materials 0.000 description 27
- 239000012530 fluid Substances 0.000 description 23
- 238000001228 spectrum Methods 0.000 description 18
- 238000003860 storage Methods 0.000 description 11
- 238000001816 cooling Methods 0.000 description 7
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 6
- 230000006835 compression Effects 0.000 description 6
- 238000007906 compression Methods 0.000 description 6
- 238000013461 design Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000010992 reflux Methods 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 150000001485 argon Chemical class 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052743 krypton Inorganic materials 0.000 description 1
- DNNSSWSSYDEUBZ-UHFFFAOYSA-N krypton atom Chemical compound [Kr] DNNSSWSSYDEUBZ-UHFFFAOYSA-N 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 229910052724 xenon Inorganic materials 0.000 description 1
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 0.000 description 1
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Abstract
本發明係有關於一種低溫分離空氣的方法,其中使用具有塔系統(10)的空氣分離設備(100),該塔系統包括高壓塔(11)、中壓塔(12)、低壓塔(13)及氬塔(14),為該高壓塔提供經壓縮且經冷卻的空氣。該高壓塔(11)的頂部氣體在蒸發或部分蒸發第一液體的情況下形成冷凝物,該第一液體提取自該高壓塔(11)並且膨脹至介於該第一與第二壓力水平之間的蒸發壓力水平,並且該冷凝物被部分或完全送回該高壓塔(11)中。蒸發該第一液體時形成第一氣體,該第一氣體部分或完全地被再壓縮至該第一壓力水平並且被送回該高壓塔(11)中。在本發明框架內,該高壓塔(11)的頂部氣體進一步在蒸發或部分蒸發第二液體的情況下形成冷凝物,該第二液體提取自該中壓塔(12)並且被壓縮至介於該第一與第二壓力水平之間的蒸發壓力水平,其中蒸發該第二液體時形成第二氣體,該第二氣體部分或完全膨脹至該第二壓力水平並且被送回該中壓塔(11)中。相應的空氣分離設備(100)同樣為本發明之主題。
Description
本發明係有關於如獨立請求項之前言所述的一種低溫分離空氣的方法及一種相應的設備。
在空氣分離設備中藉由低溫分離空氣來製造液態或氣態空氣產品,屬於習知技術且例如記載於H.-W. Häring (Hrsg.), Industrial Gases Processing, Wiley-VCH, 2006,特別是段落2.2.5,「Cryogenic Rectification」。
空氣分離設備具有精餾塔系統,傳統上,精餾塔系統可例如形成為雙塔系統,特別是經典的Linde雙塔系統,但亦可形成為三塔或多塔系統。除了用於獲取液態及/或氣態的氮及/或氧的精餾塔(即氮氧分離精餾塔)外,還可設置用於獲取其他空氣組分(尤指氪、氙及/或氬等稀有氣體)的精餾塔。其中,術語「精餾」與「蒸餾」以及「柱」與「塔」或者與此相關的複合術語往往作為同義詞使用。
上述精餾塔系統的精餾塔係在不同的壓力水平上運行。習知的雙塔系統具有所謂的高壓塔(亦稱壓力塔、中壓塔或下塔)及所謂的低壓塔(亦稱上塔)。高壓塔通常在4 bar至7 bar,特別是約5.3 bar的壓力水平上運行。低壓塔一般在1 bar至2 bar,特別是約1.4 bar的壓力水平上運行。在特定情況下,亦可在兩種精餾塔中使用更高的壓力水平。此處及下文所給出的壓力係為塔頂處的絕對壓力。
以下將為本文所說明的空氣分離設備的某些塔使用高壓塔、中壓塔及低壓塔等術語。此等術語旨在限定具有相應名稱之塔的功能,但並非根據專業文獻中為傳統空氣分離設備的塔所採用的狹隘定義。由以下闡述中可得出該等術語的含義。
本發明包括按照所謂的SPECTRA工藝對空氣進行低溫分離,該工藝記載於EP 2 789 958 A1及該案所引用的進一步專利文獻中。簡單地說,其係為一種單塔工藝。SPECTRA工藝能實現高氮產率,其研發初衷乃是為了獲得氣態加壓氮。在此以冷凝此塔之頂部氣體的方式提供被送往該塔(最簡單的情況下為唯一的塔)的回流,至此尚屬常規操作。然而在冷凝頂部氣體所用的熱交換器中,SPECTRA工藝係使用來自同一個塔的流體進行冷卻。藉由(冷)壓縮機將用於冷卻的流體的部分在用於冷卻且因此而蒸發之後回輸到精餾塔中。藉此可達到極有利的空氣係數(Luftfaktor),即每份空氣用量得到大量產品。
在SPECTRA工藝的技術方案中,可提供其他的塔以獲取其他空氣組分如純的或高純的氧及氬。由此產生經相應改良的包含附加塔的SPECTRA工藝,但其通常具有以下共同之處:如同經典SPECTRA工藝那樣,其中一個塔的頂部氣體在使用同一個塔的流體的情況下被冷凝,以形成被送往該塔的液態回流,而該流體在此過程中蒸發並且被回輸到塔中。以此方式運行的塔可為設備中工作壓力最高的那個塔,本發明即是如此。
CN 108036584 A揭露一種藉由低溫分離空氣來製造高純氮、氧及液氧的方法與一種相應的設備。充分考慮不同因素以使設備實現穩定、高效節能運行。
本發明之目的在於改良上述及下文中還將予以更詳細之闡述的SPECTRA工藝,尤其是在能耗方面。
在此背景下,本發明提出具有獨立請求項之特徵的一種低溫分離空氣的方法及一種相應的設備。技術方案分別為附屬項及以下說明的主題。
在闡述本發明的特徵與優點之前,先對本發明的一些基本原理進行詳細闡釋並對下文所使用的術語進行定義。
空氣分離設備中所使用的裝置記載於被引用的專業文獻中,例如在Häring案(見上)中記載於段落2.2.5.6「Apparatus」中。考慮到本申請框架內的用語習慣,凡若以下定義並無不同者,則明確地提請參考被引用的專業文獻。
在本案的用語習慣中,液體及氣體可能富或貧一種或數種組分,其中「富」可代表至少為75%、90%、95%、99%、99.5%、99.9%或99.99%的莫耳含量、重量含量或體積含量,「貧」可代表最高為25%、10%、5%、1%、0.1%或0.01%的莫耳含量、重量含量或體積含量。術語「佔優勢」可等同於「富」的定義。此外,液體及氣體可能富集或耗盡一種或數種組分,其中此等術語係關於用以獲取該液體或氣體的初始液體或初始氣體中的含量。以初始液體或初始氣體為參照,若液體或氣體至少含有相應組分的1.1倍、1.5倍、2倍、5倍、10倍、100倍或1000倍含量,則稱之為「富集」,若液體或氣體最多含有相應組分的0.9倍、0.5倍、0.1倍、0.01倍或0.001倍含量,則稱之為「耗盡」。舉例而言,若述及「氧」、「氮」或「氬」,則亦指富氧或富氮但並非必須僅由氧、氮或氬構成的液體或氣體。
本申請使用術語「壓力水平」及「溫度水平」來表徵壓力與溫度,此係為了表明,實現本發明理念時無需使用精確的壓力值及溫度值來說明相應設備中的相應壓力與溫度。但此等壓力與溫度通常在平均值上下1%、5%或10%之特定範圍內波動。相應的壓力水平及溫度水平可處於不相交範圍或交疊範圍。例如壓力水平尤其包含不可避免或可預見的壓力損失。溫度水平亦如此。此處以bar為單位給出的壓力水平係為絕對壓力。
若述及「膨脹機」,則一般係指習知的渦輪膨脹機。此等膨脹機特別是亦可與壓縮機耦接。此等壓縮機可尤其為渦輪壓縮機。由渦輪膨脹機與渦輪壓縮機組成的相應組合通常亦被稱為「渦輪增壓器」。在渦輪增壓器中,渦輪膨脹機與渦輪壓縮機機械耦接,其中該耦接可以轉速相同(例如透過公共軸體)或轉速不同(例如透過自有傳動裝置)之方式實現。本案為一般性地使用術語「壓縮機」。「冷壓縮機」在此係指被提供遠低於0℃,特別是低於-50℃、-75℃或-100℃及至低於-150℃或-200℃之溫度水平之流體流的壓縮機。相應的流體流特別是由主熱交換器(見下)冷卻至相應的溫度水平。
「主空氣壓縮機」係用於壓縮被提供給空氣分離設備且在該處被分離的全部空氣。而在一個或數個可酌情設置的其他壓縮機如增壓壓縮機中,則是僅對此前已在主空氣壓縮機中被壓縮過的空氣的一部分進行進一步壓縮。相應地,空氣分離設備的「主熱交換器」係為至少用於冷卻被提供給空氣分離設備且在該處被分離之空氣的佔優勢部分的熱交換器。此係至少部分地在從空氣分離設備中導出的物料流的逆流中進行。在本案的用語習慣中,以此方式從空氣分離設備中「導出的」物料流或「產品」係為不再參與設備內部循環、而是從設備內部循環被持續抽取的流體。
本發明框架內所使用的「熱交換器」可採用常規設計。熱交換器用於在至少兩個例如互為逆流而行的流體流之間間接傳熱,例如在一個熱加壓空氣流與一個或數個冷流體流之間,或者在一個酷冷液態空氣產品與一個或數個熱或較熱(視情況亦可能尚酷冷的)流體流之間。熱交換器可由單一的熱交換器段或數個並聯及/或串聯熱交換器段(例如一個或數個板式熱交換器塊)構成。例如為板式熱交換器(英文為Plate Fin Heat Exchanger)。此類熱交換器具有「通道」,該等通道形成為包含換熱面的分離式流體通路,並且平行地且被其他通道隔開地聯合成「通道組」。熱交換器之特徵在於,在熱交換器中於某個時間點上在兩種流動媒介(即,至少一個待冷卻流體流與至少一個待加熱流體流)之間進行熱交換。
「冷凝蒸發器」係指可供第一冷凝流體流與第二蒸發流體流發生間接熱交換的熱交換器。任一冷凝蒸發器皆具有液化室及蒸發室。液化室及蒸發室具有液化通道或蒸發通道。第一流體流在液化室內冷凝(液化),第二流體流在蒸發室內蒸發。蒸發室及液化室由相互之間存在熱交換關係的通道組構成。
「上」、「下」、「之上」、「之下」、「上方」、「下方」、「旁」、「並排」、「豎向」、「水平」等相對空間術語在此係關於空氣分離設備的塔正常運行時的空間定向。兩個塔或其他組件「堆疊」佈置,在此係指兩個裝置部件中的下方裝置部件的上端與兩個裝置部件中的上方裝置部件的下端處於同一大地高度或較低的大地高度,並且兩個裝置部件在水平面中的投影彼此重疊。特別地,兩個裝置部件精確地堆疊佈置,此係指兩個裝置部件的軸線在同一條豎向直線上延伸。然而,兩個裝置部件的軸線不必精確垂直地堆疊,而是亦可相對偏移,特別是在如下情況下:要求兩個裝置部件中直徑較小的裝置部件(例如塔或塔部件)與冷箱板套之間的距離與直徑較大的另一裝置部件與冷箱板套之間的距離一樣大。
與其他空氣低溫分離方法一樣,前述SPECTRA工藝(詳見下文)亦將經壓縮及預提純的空氣冷卻至適合精餾的溫度。空氣可由此而部分液化。接著,空氣被送入塔中並且在該處以傳統SPECTRA工藝在經典高壓塔的常規壓力下以前述方式被精餾,以獲得相對於大氣富集氮的頂部產品以及相對於大氣富集氧的液態底層產品。
本發明所提出的方法中亦存在相應的精餾塔,但其可在更高壓力上運行,該精餾塔在此由被稱為高壓塔的塔形成。除此之外,作為本發明框架內所使用之空氣分離設備的組成部分,亦還設有作為低壓塔在輕微的超大氣壓力水平上運行的塔以及在介於高壓塔與低壓塔之間的壓力水平上運行的中壓塔。
高壓塔、低壓塔及中壓塔在本發明框架內主要用於獲取富氧富氮空氣產品(高壓塔的頂部氣體在相應壓力下作為氮加壓產品被提供,從低壓塔中可提取底層液體作為純氧產品),而本發明所使用的其他塔則用於獲取氬,因而被稱為氬塔。與經典空氣分離設備中的氬塔一樣,此氬塔以來自低壓塔的側流為進料。其中,術語「側流」係指既非提取自底層區域(即最下面的分隔裝置下方的區域)亦非提取自頂部區域(即最上面的分隔裝置上方的區域),而是提取自二者之間(即兩個相應的分隔裝置之間)的流體流,分隔裝置例如為分隔塔板或填料區域(Packungsbereich)。
通常使用具有雙塔系統以及所謂的粗氬塔及所謂的精氬塔的空氣分離設備來獲取氬。一個例子圖示於Häring案(見上)的圖2.3A中,並且自第26頁起記載於段落「Rectification in the Low-pressure, Crude and Pure Argon Column」中以及自第29頁起記載於段落「Cryogenic Production of Pure Argon」中。若相關精餾塔採用相應設計,則原則上亦可在相應設備中棄用精氬塔。在此情況下,可從粗氬塔或一般情況下略低於傳統上被轉移至精氬塔的流體的類似塔中提取純氬,其中位於上方的分隔區域用於分離剩餘的雜質組分。本發明框架內所使用的氬塔可基本上像先前技術中的習知傳統粗氬塔(或經相應改良的粗氬塔)那樣運行。相應氬塔的設計特別是可配設相應的塔板數量。
本發明的特徵和優點
本發明總體上提出一種低溫分離空氣的方法,其中使用具有塔系統的空氣分離設備,該塔系統包括高壓塔、中壓塔、低壓塔及氬塔。如前所述,本發明框架內所使用的高壓塔的運行方式基本上與傳統SPECTRA工藝所使用的塔一樣。
本發明框架內所使用的高壓塔、中壓塔及低壓塔的特色進一步在於其各自的工作壓力水平。具體的值將在下文闡述。在本發明框架內,高壓塔在遠高於傳統高壓塔之壓力水平的壓力水平上運行。在本發明框架內,以此方式可從高壓塔提取氮產品,該氮產品可直接在相應的壓力水平上被提供,接下來不需要冷壓縮或熱壓縮。因此在本發明框架內,從設備及安全技術角度看,相應氮加壓產品的提供比經典空氣分離設備容易得多。
因此,本發明受益於習知SPECTRA工藝的優點。然而與傳統SPECTRA工藝不同,本發明亦實現了富氧空氣產品及富氬空氣產品的製造,為此需使用前述的其他塔。
總體而言,在本發明框架內,高壓塔在第一壓力水平上運行,中壓塔在低於第一壓力水平的第二壓力水平上運行,低壓塔在低於第一及第二壓力水平的第三壓力水平上運行。其中,中壓塔及低壓塔在本發明框架內亦可按空氣分離設備的傳統雙塔樣式合併。其中,用於冷凝中壓塔之頂部氣體的熱交換器亦可佈置於低壓塔的底層中。
傳統空氣分離設備所使用的雙塔系統由高壓塔與低壓塔組成,其中前述意義上的高壓塔佈置於低壓塔下方。在本發明框架內,中壓塔(佈置於低壓塔下方)及低壓塔(佈置於中壓塔上方)亦可如此。但本發明局限於此種雙柱或雙塔樣式的佈置方式。確切而言,該二塔(中壓塔與低壓塔)亦可形成為兩個分離的塔。以熱交換方式連接中壓塔與低壓塔的冷凝器亦可佈置於低壓塔外部。
在本發明框架內,中壓塔通常在與空氣分離設備的傳統高壓塔相符的壓力水平上運行。低壓塔的工作壓力水平同樣與經典低壓塔的常規工作壓力水平相符。
本發明構成習知SPECTRA工藝的一種變體,在本發明框架內,高壓塔的頂部氣體在蒸發或部分蒸發第一液體的情況下形成冷凝物,該第一液體提取自高壓塔並且膨脹至介於第一與第二壓力水平之間的蒸發壓力水平。蒸發壓力水平通常可為3 bar至7 bar。因此,該膨脹係以部分膨脹至超大氣壓力水平之形式進行,允許進一步膨脹至更低的壓力水平。
所形成的冷凝物作為回流部分或完全地被送回高壓塔中。相應冷凝物的一部分亦可作為液態富氮空氣產品從相應設備中導出。蒸發第一液體時形成第一氣體,該第一氣體部分或完全地被再壓縮至第一壓力水平並且被送回高壓塔中。此為SPECTRA工藝的重要特徵。提取自高壓塔的第一液體在本發明框架內經相應處理,該第一液體具體可為在底層上方的一些理論或實際塔板處提取自高壓塔的液體,換言之,即以側流形式從高壓塔排出的液體。
如前文中引用的專利文獻所揭露,經典SPECTRA工藝對來自高壓塔的其他物料流進行相應處理,而在本發明框架內,通常不是如此。在本發明框架內,高壓塔的頂部氣體在蒸發或部分蒸發第二液體的情況下形成頂部冷凝物,該第二液體提取自中壓塔並且被壓縮至介於第一與第二壓力水平之間的蒸發壓力水平。在冷凝頂部氣體的過程中蒸發第二液體時形成第二氣體,該第二氣體部分或完全膨脹至第二壓力水平並且被送回中壓塔中。
亦即,本發明形成兩個物料循環,其一為來自高壓塔的第一液體所經歷的物料循環,再者為來自中壓塔的液體所經歷的第二物料循環。第一循環尚與SPECTRA工藝相符,本發明所採用的第二循環相對於先前技術則具備新穎性。
為了使來自中壓塔的第二液體達到蒸發壓力水平,通常設有泵,該泵在液態下對第二液體施加壓力。來自高壓塔的第一液體通常為來自高壓塔的側流,來自中壓塔的第二液體則是在使用底層液體的情況下形成。
來自中壓塔的第二液體並非須全部被回輸到此中壓塔中。在本發明的一個技術方案(還將參考所附圖式1對此進行說明)中,如下設置:蒸發第二液體時所形成的第二氣體的一部分不被送入中壓塔中,而是特別是在與壓縮機耦接的膨脹機中進一步膨脹,最後從空氣分離設備中導出,該壓縮機用於壓縮第一氣體。
關於本發明所使用的塔的功能,再次強調:為高壓塔提供經壓縮且經冷卻的輸入空氣。這不排除亦為其他塔相應地提供空氣;但在本發明採用高壓塔的情況下,始終如此設置。
在本發明的有利技術方案中,來自高壓塔的底層液體從第一壓力水平膨脹至第二壓力水平並且被送入中壓塔中。哪怕使用了其他塔的傳統SPECTRA工藝一般情況下亦非如此;確切而言,在此類傳統工藝中,使用底層液體而形成的相應物料流將同樣用作冷卻劑以冷凝相應塔的頂部氣體。
在本發明所提出的方法的有利技術方案中,液態提取自高壓塔的側流部分或完全地從第一壓力水平膨脹至第二壓力水平,並且在形成液體部分及氣體部分的情況下被送去作相分離處理。其中,液體部分可特別是部分或完全地在低壓塔中進行分離,氣體部分部分或完全地在中壓塔中進行分離。此種工藝的一個特殊技術方案包括:將提取自高壓塔的側流或該側流的從第一壓力水平膨脹至第二壓力水平的部分送入中壓塔進行相分離,在中壓塔中,液體部分液態沉積到例如阻液容器中或沉積在分隔塔板上,氣體部分直接轉變為氣相。以此方式可再度從中壓塔部分或完全地提取液體部分,並將其送入低壓塔中,液體部分在低壓塔中進行分離。氣體部分留在中壓塔中並在該處進行分離。
如前所述,在本發明一個有利技術方案的框架內,所使用的氬塔基本上按空氣分離設備的傳統氬塔的方式進行工作。意即:在本發明框架內,亦從低壓塔提取富集氬的側流,其中將來自低壓塔的第二流的至少一部分送入氬塔中。富集氬的側流特別是具有比存在於低壓塔頂部或底層的側流更高的氬含量。在空氣分離設備領域基本上已知的有利區域上從低壓塔提取該側流。
在本發明框架內,有利地僅將該側流的一部分轉移到氬塔中,而非將該側流直接送入氬塔。這有利地藉由以下方式而實現:將側流部分或完全地提供給氧塔,在氧塔中形成相對於側流富集氬的物料流,將該物料流部分或完全地送入氬塔中,藉此將來自低壓塔的側流的一部分送入氬塔中。
在本發明一個有利技術方案的框架內,氬塔在使用頂部冷凝器的情況下進行工作。這只意味著:氬塔的頂部氣體在部分蒸發液體的情況下形成冷凝物,該冷凝物部分或完全地被送回氬塔中。其中,因部分蒸發而使得氬塔的頂部氣體形成冷凝物的液體在本發明框架內有利地提取自中壓塔,此為相對於習知工藝的另一根本區別。作為替代方案,部分蒸發時所形成的氣體及/或部分蒸發時所剩餘的液體可部分或完全地被送入低壓塔中。
由SPECTRA工藝基本上已知,在本發明框架內可使用與壓縮機耦接的膨脹機。因此,可使用壓縮機來對第一氣體或第一氣體的被再壓縮至第一壓力水平且被送回高壓塔的部分進行再壓縮,該壓縮機與膨脹機機械耦接,該膨脹機用於使第二氣體的未被送回中壓塔的另一部分膨脹。
本發明還有關於一種空氣分離設備,關於其具體特徵,請參閱相應的獨立請求項。關於此種設備進一步的特徵與技術方案及較佳實施方式,明確地提請參閱上文中有關本發明之方法及其有利技術方案的說明。此種空氣分離設備有利地用於實施上文以不同技術方案所闡述的方法。
下面將參考所附圖式對本發明進行詳細闡述,所附圖式圖示根據本發明之技術方案的空氣分離設備。
圖1以高度簡化的工藝流程示意圖之形式圖示根據本發明的尤佳實施方式的空氣分離設備,其整體上用100標示。
圖1中所圖示的空氣分離設備100透過過濾器101並藉由主空氣壓縮機102從在此一般性地以A標示的大氣中吸入空氣,該主空氣壓縮機特別是採用多級設計且帶有中間冷卻器。在熱交換器103及104中經再冷卻後,以此方式形成的輸入空氣流a在以水W運行的直接接觸式冷卻器105中被冷卻,而後被提供給吸附裝置106。
在輸入空氣流a以此方式乾燥並基本上去除二氧化碳之後,將輸入空氣流提供給主熱交換器107。在靠近主熱交換器的冷端處從主熱交換器提取輸入空氣流a,並且在此處所圖示的示例中,將輸入空氣流基本上提供給整體以10標示的塔系統的高壓塔11。圖中未單獨示出的部分在需要時可經旁路分岔出去。
高壓塔11的頂部流b的一部分可以物料流c之形式作為氣態加壓氮產品從空氣分離設備100導出。相應的加壓氮產品再次以C1及C2標示。在此處所圖示的示例中,頂部流b的未以此方式從空氣分離設備導出的部分則以物料流d的形式被提供給熱交換器或者說冷凝器108,並且在該處基本上被冷凝。相應冷凝物的一部分可以物料流e的形式作為液態回流被回輸到高壓塔11上。另一部分以沖洗流P的形式被提取。需要時亦可以此處所圖示的方式在設備100中送入液氮E。另一部分可以物料流f的形式在過冷器109中被過度冷卻並且作為液氮產品F從設備中被導出。用於過度冷卻的、在過冷器109下游分岔出去的部分作為殘餘氣體從設備中被導出,下文還將參考其他物料流對此進行闡述。
在圖示示例中,以高壓塔11的底層流g為塔系統10的中壓塔12供料。為此,此底層流g在主熱交換器107中被冷卻,而後在底層上方或者說在一些位於底層上方的分隔塔板上方被送入中壓塔。
以來自高壓塔11的側流h為中壓塔進一步供料,該側流膨脹進入中壓塔12。以此方式形成的氣體留在中壓塔12中;物料流i形式的液體則在饋送點正下方至少部分地再度從中壓塔12被提取,並且先穿過過冷器110,再被送入塔系統10的低壓塔13。
首先使用提取自高壓塔的側流k來運行熱交換器108。此側流先在主熱交換器107中被進一步冷卻,再被提供給熱交換器108。此時發生部分膨脹。在熱交換器108下游,相應蒸發的流體的一部分可被排放到大氣A中。另一部分(在此仍被圖示為物料流k)視情況在與其他物料流合併後在壓縮機111中被再壓縮,該壓縮機與膨脹機112機械耦接並且進一步藉由耗散制動器被制動。物料流k可以此方式重新被送入高壓塔11中。用於熱交換器108的進一步製冷量由中壓塔12的底層流I提供。為此,藉由泵113使該底層流達到熱交換器108中所需要的壓力水平。
物料流I在熱交換器108中蒸發後以第一分流m的形式在主熱交換器107中被加熱並且至少部分地在膨脹機112中膨脹。此物料流接下來將特別是與來自高壓塔的頂部流b的在過冷器109中起冷卻作用的部分一起從設備中被導出。來自中壓塔12的在熱交換器108中蒸發的底層流的另一部分n則被回輸到中壓塔12中。
空氣分離設備100還包括氬塔14,該氬塔最後由低壓塔13供料或者說以提取自低壓塔13的側流o為進料。但在圖示示例中,側流o並非直接轉移到氬塔14中,而是先轉移到整體以15標示的氧塔的上部15a中。在上部15a中,物料流o或者說以此方式轉移到上部15a中的流體進一步地富集氬並耗盡氧,使得相應的物料流p可從上部15a的頂部轉移到氬塔14中。來自氬塔14的底層液體被此處未單獨標示的泵回輸到氧塔的上部15a中。
包括上部15a與下部15b的氧塔15藉由底層蒸發器151進行工作。此底層蒸發器151及佈置於低壓塔13的底層中的底層蒸發器131分別用於冷凝中壓塔12的頂部氣體,該頂部氣體以物料流q之形式提取自中壓塔。在此未被單獨且個別示出的冷凝部分基本上用作被送往中壓塔12及低壓塔13的回流。
從低壓塔13的頂部抽取物料流r,該物料流以不純氧的形式經加熱後被排放到大氣中或另作他用。
從低壓塔13的底層提取氧流s及t,其中氧流s在未單獨標示的泵中被內壓縮並且可用於提供相應的內壓縮產品S。氧流t則可被加熱並且可被排出設備或者說排放到大氣中。如此處以關聯符X之形式所示,一部分可被回輸到低壓塔13中。
頂部由頂部冷凝器141冷卻的氬塔14可用於提供液氬流u,該液氬流可例如在儲罐系統T中經暫存後作為內壓縮氬產品U被提供。其中一部分亦可長期儲存於儲罐T1中並且例如呈液態地從設備中排出。
在此處所圖示的示例中,使用物料流v來冷卻氬塔14的頂部冷凝器141,該物料流係在底層上方的一些塔板處液態提取自中壓塔12並且被送入氬冷凝器141的蒸發室中。此處的已蒸發及未蒸發部分可以圖示方式被回輸到低壓塔中。
如此處以相應的流體箭頭之形式所示,氧塔15的上部15a與下部15b彼此流體耦合。耗盡氬且富集氧的流體從上部15a轉移到下部15b中並且在該處被進一步精餾。藉此方式可從氧塔15的底層或者說從氧塔下部提取純氧流w,該純氧流同樣可經由相應的儲罐系統t2或t3作為高純氧產品W以內壓縮形式被排出空氣分離設備100。此處所圖示的其他物料流及其在空氣分離設備100中的具體處理可直接從圖式中獲得。
10:塔系統
11:高壓塔
12:中壓塔
13:低壓塔
14:氬塔
15:氧塔
15a:上部
15b:下部
100:空氣分離設備
101:過濾器
102:主空氣壓縮機
103:熱交換器
104:熱交換器
105:直接接觸式冷卻器
106:吸附裝置
107:主熱交換器
108:冷凝器/熱交換器
109:過冷器
110:過冷器
111:壓縮機
112:膨脹機
113:泵
131:底層蒸發器
141:頂部冷凝器/氬冷凝器
151:底層蒸發器
A:大氣
a:輸入空氣流
b:頂部流
C1:加壓氮產品
C2:加壓氮產品
c:物料流
d:物料流
E:液氮
e:物料流
F:液氮產品
f:物料流
g:底層流
h:側流
I:底層流/物料流
i:物料流
k:側流/物料流
m:第一分流
n:另一部分
o:側流/物料流
P:沖洗流
p:物料流
q:物料流
r:物料流
S:內壓縮產品
s:氧流
T:儲罐系統
T1:儲罐
t:氧流
t2:儲罐系統
t3:儲罐系統
U:內壓縮氬產品
u:液氬流
v:物料流
W:水/高純氧產品
w:純氧流
X:關聯符
〔圖1〕以簡化工藝流程圖的形式圖示根據本發明之技術方案的空氣分離設備。
10:塔系統
11:高壓塔
12:中壓塔
13:低壓塔
14:氬塔
15:氧塔
15a:上部
15b:下部
100:空氣分離設備
101:過濾器
102:主空氣壓縮機
103:熱交換器
104:熱交換器
105:直接接觸式冷卻器
106:吸附裝置
107:主熱交換器
108:冷凝器/熱交換器
109:過冷器
110:過冷器
111:壓縮機
112:膨脹機
113:泵
131:底層蒸發器
141:頂部冷凝器/氬冷凝器
151:底層蒸發器
A:大氣
a:輸入空氣流
b:頂部流
C1:加壓氮產品
C2:加壓氮產品
c:物料流
d:物料流
E:液氮
e:物料流
F:液氮產品
f:物料流
g:底層流
h:側流
I:底層流/物料流
i:物料流
k:側流/物料流
m:第一分流
n:另一部分
o:側流/物料流
P:沖洗流
p:物料流
q:物料流
r:物料流
S:內壓縮產品
s:氧流
T:儲罐系統
T1:儲罐
t:氧流
t2:儲罐系統
t3:儲罐系統
U:內壓縮氬產品
u:液氬流
v:物料流
W:水/高純氧產品
w:純氧流
X:關聯符
Claims (9)
- 一種低溫分離空氣的方法,其中, - 使用具有塔系統(10)的空氣分離設備(100),該塔系統包括高壓塔(11)、中壓塔(12)、低壓塔(13)及氬塔(14), - 該高壓塔(11)在第一壓力水平上運行,該中壓塔(12)在低於該第一壓力水平的第二壓力水平上運行,該低壓塔(13)在低於該第二壓力水平的第三壓力水平上運行, - 為該高壓塔(11)提供經壓縮且經冷卻的空氣,並且 - 該高壓塔(11)的頂部氣體在蒸發或部分蒸發第一液體的情況下形成冷凝物,該第一液體提取自該高壓塔(11)並且膨脹至介於該第一與第二壓力水平之間的蒸發壓力水平,並且該冷凝物被部分或完全送回該高壓塔(11)中,其中蒸發該第一液體時形成第一氣體,該第一氣體部分或完全地被再壓縮至該第一壓力水平並且被送回該高壓塔(11)中, 其特徵在於, - 該高壓塔(11)的頂部氣體在蒸發或部分蒸發第二液體的情況下形成冷凝物,該第二液體提取自該中壓塔(12)並且達到介於該第一與第二壓力水平之間的蒸發壓力水平,並且 - 蒸發該第二液體時形成第二氣體,該第二氣體部分或完全膨脹至該第二壓力水平並且被送回該中壓塔(11)中。
- 如請求項1所述之方法,其中,來自該高壓塔(11)的底層液體從該第一壓力水平膨脹至該第二壓力水平並且被送入該中壓塔(12)中。
- 如請求項1或2所述之方法,其中,液態提取自該高壓塔(11)的側流部分或完全地從該第一壓力水平膨脹至該第二壓力水平,並且在形成液體部分及氣體部分的情況下被送去作相分離處理,其中該液體部分部分或完全地在該低壓塔(13)中進行分離,該氣體部分部分或完全地在該中壓塔(12)中進行分離。
- 如請求項3所述之方法,其中,將提取自該高壓塔(11)的該側流或該側流的從該第一壓力水平膨脹至該第二壓力水平的部分送入該中壓塔(12)進行相分離,其中再度從該中壓塔(12)部分或完全地提取該液體部分,並將其送入該低壓塔(13)中,且其中將該氣體部分留在該中壓塔(12)中。
- 如前述請求項中任一項所述之方法,其中,從該低壓塔(13)提取富集氬的側流,其中將來自該低壓塔(13)的該側流的至少一部分送入該氬塔(14)中。
- 如請求項5所述之方法,其中,以如下方式將來自該低壓塔(13)的該側流的一部分送入該氬塔(14)中:將該側流部分或完全地提供給氧塔(15),在該氧塔中形成相對於該側流富集氬的物料流,將該物料流部分或完全地轉移到該氬塔(14)中。
- 如前述請求項中任一項所述之方法,其中,該氬塔(14)的頂部氣體在部分蒸發液體的情況下形成冷凝物,該冷凝物部分或完全地被送回該氬塔(14)中,其中,因部分蒸發而使得該氬塔(14)的頂部氣體形成該冷凝物的該液體提取自該中壓塔(12),或者其中,部分蒸發時所形成的氣體及/或部分蒸發時所剩餘的液體部分或完全地被送入該低壓塔(13)中。
- 如前述請求項中任一項所述之方法,其中,使用壓縮機來對該第一氣體或該第一氣體的被再壓縮至該第一壓力水平且被送回該高壓塔(11)的部分進行再壓縮,該壓縮機與膨脹機機械耦接,該膨脹機用於使該第二氣體的未被送回該中壓塔(11)的另一部分膨脹。
- 一種空氣分離設備(100),具有塔系統(10),該塔系統包括高壓塔(11)、中壓塔(12)、低壓塔(13)及氬塔(14),其中該空氣分離設備(100)被建構為用於: - 在第一壓力水平上運行該高壓塔(11),在低於該第一壓力水平的第二壓力水平上運行該中壓塔(12),在低於該第一及第二壓力水平的第三壓力水平上運行該低壓塔(13), - 為該高壓塔(11)提供經壓縮且經冷卻的空氣, - 在蒸發或部分蒸發第一液體的情況下使該高壓塔(11)的頂部氣體形成冷凝物,該第一液體提取自該高壓塔(11)並且膨脹至介於該第一與第二壓力水平之間的蒸發壓力水平,並且將該冷凝物部分或完全送回該高壓塔(11)中,將蒸發該第一液體時所形成的第一氣體部分或完全地再壓縮至該第一壓力水平並且送回該高壓塔(11)中, 其特徵在於構件,該等構件被建構為用於: - 蒸發或部分蒸發第二液體以使該高壓塔(11)的頂部氣體形成冷凝物,該第二液體提取自該中壓塔(12)並且被壓縮至介於該第一與第二壓力水平之間的蒸發壓力水平,使蒸發該第二液體時所形成的第二氣體部分或完全膨脹至該第二壓力水平並且將其送回該中壓塔(11)中。
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