TW201726899A - 利用後端渦輪膨脹機自精煉廢氣回收所欲輕烴之系統及方法 - Google Patents

利用後端渦輪膨脹機自精煉廢氣回收所欲輕烴之系統及方法 Download PDF

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TW201726899A
TW201726899A TW105141800A TW105141800A TW201726899A TW 201726899 A TW201726899 A TW 201726899A TW 105141800 A TW105141800 A TW 105141800A TW 105141800 A TW105141800 A TW 105141800A TW 201726899 A TW201726899 A TW 201726899A
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distillation column
liquid
light hydrocarbons
gas
product
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博 葛布吉安
蘇迪爾 戈利克利
杰 游
國堅 梁
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貝特烴溶劑科技公司
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Abstract

本發明係關於利用後端渦輪膨脹機自精煉廢氣回收輕烴以生成更高回收率之該等輕烴以用作石油化學原料及在液相輕烴進入該渦輪膨脹機之前移除液相輕烴的系統及方法。

Description

利用後端渦輪膨脹機自精煉廢氣回收所欲輕烴之系統及方法
本發明總體而言係關於利用後端渦輪膨脹機自精煉廢氣回收所欲輕烴之系統及方法。更具體言之，本發明係關於利用後端渦輪膨脹機自精煉廢氣回收所欲輕烴，以生成更高回收率之該等輕烴以用作石油化學原料及在較重烴進入該渦輪膨脹機之前移除較重烴。
來自工業應用、尤其精煉烴操作中之氣流之氣體常常包括甲烷、其他成分及具有等於或大於乙烯之分子量之輕烴，該等輕烴包括乙烯、乙烷、丙烯、丙烷、丁烯及丁烷(下文統稱為「所欲輕烴」)。所欲輕烴之回收為較佳的，因為所欲輕烴作為石油化學原料比作為精煉燃料氣體更加有價值。然而，回收所欲輕烴之系統及方法有侷限性。 在不同精煉裝置中，諸如飽和氣體設備、焦化乾氣設備及流體催化裂化器(FCC)氣體設備(統稱為「精煉氣體設備」)中，所欲輕烴之當前回收利用吸收-汽提實現。利用吸收-汽提之丙烷回收率在90-94%範圍內，而通常不回收乙烷。 最近，已利用低溫系統自精煉廢氣回收所欲輕烴中的一些。該等低溫系統之一般組態由首先壓縮、冷卻及乾燥饋料氣體以獲得經處理氣體，繼而經由渦輪膨脹機處理該經處理氣體以生成兩相產物構成。在該渦輪膨脹機中達到該等低溫系統之最低溫度。自穿過渦輪膨脹機之經處理氣體產生之液體與蒸氣分離且經傳送至蒸餾塔中，以分離所欲輕烴與甲烷及其他輕成分。將塔頂蒸氣及渦輪膨脹機蒸氣用作精煉燃料氣體。利用此方法之乙烷回收率通常不超過80%。 習知的低溫系統具有缺點。在經處理氣體中存在重烴可能導致在渦輪膨脹機內不希望的凝固，從而使該低溫系統之運作失敗。此外，在習知系統中回收所欲輕烴之效率為有限的。
本發明藉由提供利用後端渦輪膨脹機自精煉廢氣回收所欲輕烴以生成更高回收率之所欲輕烴以用作石油化學原料及在重烴進入該渦輪膨脹機之前移除重烴之系統及方法來克服先前技術中之一或多個缺陷。 在一個實施例中，本發明包括用於回收輕烴之系統，其包括氣體冷卻器/乾燥器及連接至該氣體冷卻器/乾燥器以用於回收輕烴之蒸餾塔。 在另一實施例中，本發明包括自氣流回收輕烴之方法，其包括藉由壓縮、胺處理、乾燥及冷卻處理該氣流以生成殘餘較輕氣體，及在塔頂產物與含有輕烴之粗製塔底液體產物之間在蒸餾塔中分離該殘餘較輕氣體。 根據各種實施例及相關圖式之下列描述，本發明之其他態樣、優點及實施例將對熟習此項技術者變得顯而易見。
本發明之主題被特異性地描述；然而，該描述自身並非意圖限制本發明之範疇。因此該主題亦可能以其他方式體現，以包括不同步驟或類似於本文所述步驟之步驟之組合，以及其他當前技術或未來技術。此外，雖然本文中可使用術語「步驟」來描述所用方法之不同要素，但該術語不應被解釋為意指本文中所揭示之各個步驟之中或之間的任何特定順序，除非另外明確地藉由對特定順序之描述加以限制。雖然以下描述涉及精煉氣體設備，但本發明之系統及方法不限於此且可在其他精煉廠中應用以達成類似結果。 現參看圖 1 ，示意圖展示了用於在精煉氣體設備中利用後端渦輪膨脹機自廢氣回收所欲輕烴之系統100 。 自煉焦器或FCC主分餾器頂罐或自任何其他來源(諸如精煉氣體流、用作燃料或欲作為廢料移除之氣體流)獲得含有輕烴之原料饋料氣體。該原料饋料氣體通過原料饋料氣體管線104 提供至氣體冷卻器/乾燥器106 。在該氣體冷卻器/乾燥器106 中，將該原料饋料氣體壓縮，胺處理以移除硫化氫及二氧化碳，必要時乾燥且冷卻以生成殘餘較輕氣體。該殘餘較輕氣體接著在流出口通過殘餘較輕氣體管線110 進給至蒸餾塔112 。該蒸餾塔112 包括蒸餾塔頂部部分112a 、蒸餾塔底部部分112c 及蒸餾塔中間部分112d 。蒸餾塔中間部分112d 係在蒸餾塔頂部部分112a 及蒸餾塔底部部分112c 中間。在蒸餾塔112 中，自該殘餘較輕氣體中移除該所欲輕烴以生成粗製塔底液體產物，及包含甲烷及較輕成分之塔頂產物。 該粗製塔底液體產物的一部分通過粗製塔底液體產物管線145a 離開蒸餾塔底部部分112c 。系統100 亦包括再沸器142 ，其通過粗製塔底液體產物管線145b 自蒸餾塔112 的底部部分112c 抽取粗製塔底液體產物之另一部分。再沸器142 加熱且再循環蒸餾塔底部部分112c 之粗製塔底液體產物。  塔頂產物(已自其中移除所欲輕烴中的一些的經處理氣體)通過塔頂產物管線116 在蒸餾塔頂部部分112a 處離開該蒸餾塔112 ，且首先經傳送至諸如液氣分離器(Knock out drum)之第一液體/氣體分離器118 中，以移除可能存在於塔頂產物中之小體積之液體，從而阻止該液體進入後端渦輪膨脹機120 。否則後端渦輪膨脹機120 將凍結任何液體，干擾後端渦輪膨脹機120 之運作。剩餘的塔頂產物接著傳遞至後端渦輪膨脹機120 中，在其中該塔頂產物經進一步冷卻以生成含有冷凝液體及剩餘蒸氣之渦輪膨脹機兩相產物，該冷凝液體充當蒸餾塔112 之回流。渦輪膨脹機兩相產物通過渦輪膨脹機兩相產物管線124 傳輸至諸如液氣分離器之第二液體/氣體分離器126 中，在其中該渦輪膨脹機兩相產物經分離成冷凝液體及剩餘蒸氣。該冷凝液體通過冷凝液體管線132 傳送至泵134 中且接著作為回流傳送至該蒸餾塔頂部部分112a 中。 剩餘蒸氣通過剩餘蒸氣管線130 傳送至殼體之殼體側及位於蒸餾塔112 中接近蒸餾塔頂部部分112a 之第一管式冷凝器112b 中，以實現在蒸餾塔112 內間接冷卻蒸餾塔蒸氣及作為殘餘氣體離開。該第一管式冷凝器112b 提高蒸餾塔在分離殘餘氣體之成分方面之效率。該第一管式冷凝器112b 可由在蒸餾塔112 之殼體內間隔開的豎直冷凝器管構成，其中在蒸餾塔112 中塔內部蒸氣可流入冷凝器管內。該第一管式冷凝器112b 與剩餘蒸氣管線130 連通，以使得剩餘蒸氣經饋入至在豎直冷凝器管之間的空隙中。來自剩餘蒸氣管線130 之剩餘蒸氣的溫度低於在蒸餾塔112 內之塔內部蒸氣之溫度，使得該剩餘蒸氣充當冷卻介質。當穿過第一管式冷凝器112b 之豎直冷凝器管之間的空隙時，剩餘蒸氣自蒸餾塔112 內的塔內部蒸氣吸收熱量，且作為經加熱之剩餘蒸氣離開。利用原本將作為廢料的剩餘蒸氣作為第一管式冷凝器112b 中之冷卻介質能最大化剩餘蒸氣之有限值。 在另一實施例中，蒸餾塔112 可為去乙烷塔。 為了進一步提高去乙烷塔蒸餾塔112 之效率，第二冷凝器150 可設置在蒸餾塔中間部分112d 上方。該第二冷凝器150 允許自蒸餾塔112 之經加熱的內容物傳遞熱，從而提高蒸餾速率且因此提高蒸餾塔112 之效率。經冷卻之製冷劑152 經提供至該第二冷凝器150 中且作為經加熱之製冷劑154 經移除。該第二冷凝器150 連同用於自蒸餾塔112 內提供材料且將材料提供回蒸餾塔112 中之管路及抽汲系統可在蒸餾塔外部。較佳地，該第二冷凝器150 在蒸餾塔112 內部和以內，使得外部組件可減到最少。 該第二冷凝器150 可由在蒸餾塔112 之殼體內間隔開的豎直管構成，其中在蒸餾塔112 中塔內部蒸氣可流入冷凝器管內。溫度低於蒸餾塔112 內之殘餘氣體溫度的經冷卻之製冷劑152 經饋入至蒸餾塔112 內之冷凝器管之間的空間中以充當冷卻介質。當穿過第二冷凝器150 之豎直冷凝器管之間的空隙時，經冷卻之製冷劑152 自蒸餾塔112 內之塔內部蒸氣吸收熱量，且作為經加熱之製冷劑154 離開。經加熱之製冷劑154 接著經壓縮，冷凝，膨脹，且作為冷卻器製冷劑152 返回至第二冷凝器150 中。 現參看圖 2 ，示意圖展示了利用後端渦輪膨脹機及熱交換器自廢氣回收某些輕烴之另一系統200 。蒸餾塔112 可為去甲烷塔。與去甲烷塔一致，系統200 進一步包括在蒸餾塔中間部分112d 中與蒸餾塔112 連通之熱交換器202 。熱交換器202 自蒸餾塔中間部分112d 中抽取部分蒸餾液體之一部分，加熱部分蒸餾液體之該部分以生成部分蒸餾液體之經加熱部分，及提供部分蒸餾液體之該經加熱部分至蒸餾塔112 之蒸餾塔中間部分112d 中。 系統100 可自精煉氣體設備之進料提供更高回收率之所欲輕烴，尤其丙烷及丙烯，與習知吸收器-汽提器氣體設備之90-94%回收率相比，該更高回收率高達99%。此外，若需要回收乙烯及乙烷，則該等成分之回收率可高達50%。與渦輪膨脹機安置於蒸餾塔與氣體冷卻器/乾燥器之間的習知組態相比，系統200 可自精煉廢氣提供甚至更高的乙烯及乙烷回收率，在3-5%範圍內。各系統亦在液體及重氣體烴進入渦輪膨脹機之前移除液體及重氣體烴，其在渦輪膨脹機中很可能凍結。所揭示之各系統可置換使用於精煉氣體設備中用於回收所欲輕烴之習知吸收器-汽提器設計。各系統亦可經翻新成現有精煉氣體設備。利用任一系統之低溫氣體設備都將提供更高的丙烷回收率且將允許回收氣體設備進料中之乙烷部分。 雖然已結合當前較佳實施例描述了本發明，但熟習此項技術者將理解其並不意欲將本發明限於彼等實施例。舉例而言，預期藉由不同地導引某些氣流或藉由調節操作參數，可得到不同的優化及效率，然而這不會導致該系統落在本發明之範疇以外。因此預期可獲得各種替代實施例及對所揭示之實施例進行修改而不會背離由隨附申請專利範圍及其等效物所限定之本發明之精神及範疇。
100‧‧‧系統
104‧‧‧原料饋料氣體管線
106‧‧‧氣體冷卻器/乾燥器
110‧‧‧殘餘較輕氣體管線
112‧‧‧蒸餾塔
112a‧‧‧蒸餾塔頂部部分
112b‧‧‧第一管式冷凝器
112c‧‧‧蒸餾塔底部部分
112d‧‧‧蒸餾塔中間部分
116‧‧‧塔頂產物管線
118‧‧‧第一液體/氣體分離器
120‧‧‧後端渦輪膨脹機
124‧‧‧渦輪膨脹機兩相產物管線
126‧‧‧第二液體/氣體分離器
130‧‧‧剩餘蒸氣管線
132‧‧‧冷凝液體管線
134‧‧‧泵
142‧‧‧再沸器
145a‧‧‧粗製塔底液體產物管線
145b‧‧‧粗製塔底液體產物管線
150‧‧‧第二冷凝器
152‧‧‧經冷卻之製冷劑
154‧‧‧經加熱之製冷劑
200‧‧‧系統
202‧‧‧熱交換器
下文將參考附圖描述本發明，其中相同的部件參考相同的編號，其中：圖 1 為說明利用後端渦輪膨脹機自精煉廢氣回收輕烴之系統的示意圖。圖 2 為說明利用後端渦輪膨脹機及熱交換器自精煉廢氣回收輕烴之另一系統的示意圖。
100‧‧‧系統
104‧‧‧原料饋料氣體管線
106‧‧‧氣體冷卻器/乾燥器
110‧‧‧殘餘較輕氣體管線
112‧‧‧蒸餾塔
112a‧‧‧蒸餾塔頂部部分
112b‧‧‧第一管式冷凝器
112c‧‧‧蒸餾塔底部部分
112d‧‧‧蒸餾塔中間部分
116‧‧‧塔頂產物管線
118‧‧‧第一液體/氣體分離器
120‧‧‧後端渦輪膨脹機
124‧‧‧渦輪膨脹機兩相產物管線
126‧‧‧第二液體/氣體分離器
130‧‧‧剩餘蒸氣管線
132‧‧‧冷凝液體管線
134‧‧‧泵
142‧‧‧再沸器
145a‧‧‧粗製塔底液體產物管線
145b‧‧‧粗製塔底液體產物管線
150‧‧‧第二冷凝器
152‧‧‧經冷卻之製冷劑
154‧‧‧經加熱之製冷劑

Claims (16)

  1. 一種用於回收輕烴之系統，其包括： 氣體冷卻器/乾燥器；及 連接至該氣體冷卻器/乾燥器以用於回收該等輕烴之蒸餾塔。
  2. 如請求項1之系統，進一步包含 連接至該蒸餾塔以用於分離液態輕烴與氣態輕烴之第一液體/氣體分離器；及 連接至該第一液體/氣體分離器以用於冷卻氣態輕烴來生成冷凝液體及剩餘蒸氣之渦輪膨脹機。
  3. 如請求項2之系統，進一步包含 連接至該渦輪膨脹機以用於分離該冷凝液體與該剩餘蒸氣之第二液體/氣體分離器； 連接至該第二液體/氣體分離器以用於傳輸該剩餘蒸氣之剩餘蒸氣管線； 連接至該剩餘蒸氣管線以用於利用該剩餘蒸氣冷卻該蒸餾塔之第一冷凝器； 連接至該第二液體/氣體分離器以用於傳輸該冷凝液體至該蒸餾塔中來用於進一步處理之冷凝液體管線；及 與該蒸餾塔連通以用於移除該等輕烴之產物管線。
  4. 如請求項1之系統，其中該蒸餾塔為去乙烷塔。
  5. 如請求項3之系統，進一步包含： 在該蒸餾塔中用於利用經冷卻之製冷劑冷卻該蒸餾塔的第二冷凝器。
  6. 如請求項1之系統，其中該蒸餾塔為去甲烷塔。
  7. 如請求項5之系統，進一步包含： 與在蒸餾塔中之該等輕烴連通之熱交換器。
  8. 如請求項1之系統，其中該等輕烴包含乙烯及分子量大於乙烯之輕烴。
  9. 一種自氣流回收輕烴之方法，其包含： 藉由壓縮、胺處理、乾燥及冷卻處理該氣流以生成殘餘較輕氣體；及 在蒸餾塔中在塔頂產物與含有該等輕烴之粗製塔底液體產物之間分離該殘餘較輕氣體。
  10. 如請求項9之方法，進一步包含： 在該渦輪膨脹機中處理之前自該塔頂產物移除液體； 通過渦輪膨脹機處理該塔頂產物以獲得冷凝液體及剩餘蒸氣； 在使該冷凝液體返回至該蒸餾塔之步驟之前分離該冷凝液體及剩餘蒸氣； 使該冷凝液體返回至該蒸餾塔中；及 使該剩餘蒸氣流過該蒸餾塔中之第一冷凝器。
  11. 如請求項10之方法，進一步包含： 在第一熱交換器中加熱該粗製塔底液體產物之一部分以獲得粗製塔底液體產物之經加熱部分；及 將粗製塔底液體產物之該經加熱部分注入該蒸餾塔中。
  12. 如請求項9之方法，其中該蒸餾塔為去乙烷塔。
  13. 如請求項11之方法，進一步包含： 向該蒸餾塔中之第二冷凝器提供經冷卻之製冷劑。
  14. 如請求項9之方法，其中該蒸餾塔為去甲烷塔。
  15. 如請求項14之方法，進一步包含： 在第一熱交換器中加熱該粗製塔底液體產物之一部分以獲得粗製塔底液體產物之經加熱部分；及 將粗製塔底液體產物之該經加熱部分注入該蒸餾塔中。
  16. 如請求項15之方法，進一步包含： 在第二熱交換器中加熱該粗製塔底液體產物之一部分以獲得粗製塔底液體產物之第二經加熱部分；及 將粗製塔底液體產物之該第二經加熱部分注入該蒸餾塔中。
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