TWI564475B - 低排放之三循環動力產生系統和方法 - Google Patents

低排放之三循環動力產生系統和方法 Download PDF

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TWI564475B
TWI564475B TW100120161A TW100120161A TWI564475B TW I564475 B TWI564475 B TW I564475B TW 100120161 A TW100120161 A TW 100120161A TW 100120161 A TW100120161 A TW 100120161A TW I564475 B TWI564475 B TW I564475B
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羅素 歐福克
摩西斯 密塔
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艾克頌美孚上游研究公司
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    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/34—Gas-turbine plants characterised by the use of combustion products as the working fluid with recycling of part of the working fluid, i.e. semi-closed cycles with combustion products in the closed part of the cycle
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Description

低排放之三循環動力產生系統和方法 相關申請案的交互參考
本申請案根據2010年7月2日提出之美國臨時專利申請案第61/361,173號請求優先權，其標題為低排放之三循環動力產生系統及方法，以提及方式完全納入本文。
本申請案包含的主旨係關於2010年7月2日提出的美國專利申請案第61/361,169號標題為「控制燃料燃燒的系統及方法」；2010年7月2日提出的美國專利申請案第61/361,170號標題為「低排放之三循環動力產生系統及方法」；2010年7月2日提出的美國專利申請案第61/361,176號標題為「以排氣循環及直接接觸冷卻器之化學計量燃燒」；2010年7月2日提出的美國專利申請案第61/361,178號標題為「以排氣循環之富含空氣的化學計量燃燒」；及2010年7月2日提出的美國專利申請案第61/361,180號標題為「低排放動力產生系統及方法」。
本揭示的具體實例係關於複合循環動力系統中的低排放動力產生。更特別的是，本揭示的具體實例係關於加強CO2製造及捕捉之化學計量地燃燒燃料的方法及設備，及富氮氣體的膨脹或壓縮。
本單元係要介紹本技藝的各種觀點，其與本揭示的示範性具體實例相關。相信本討論是要輔助提供能促進對本揭示特殊觀點的較佳瞭解之架構。因此，應瞭解應以此見解閱讀本單元，且非必需受先前技藝所允許。
許多產油國家正遭遇國內動力需求的強烈成長，且具有加強油回收(EOR)的興趣以增進其貯油層的油回收。二種常見的EOR技術包括用於油層壓力維持的氮(N2)注射及用於EOR的混相沖排油的二氧化碳(CO2)注射。其也會有全球所關切的溫室氣體(GHG)排放。此關切與許多國家之覆蓋及交易(cap-and trade)政策執行結合，使得在這些及其他國家以及操作烴生產系統的公司將降低CO2排放列為優先事項。
一些降低CO2排放的方法包括燃料去碳化或使用例如胺類的溶劑之後燃燒捕捉。然而，此二種解決方法昂貴且降低動力產生效率，導致較低的動力產生、增加燃料需求及增加電力成本，以符合國內的動力需求。特別是存在氧、SOx及NOx成份時，使得胺溶劑吸收的使用很有問題。另一方法為在複合循環中之含氧燃料(oxyfuel)的燃氣渦輪(例如在此將來自燃氣渦輪布雷頓(Brayton)循環的廢熱捕捉以製造蒸汽，及在蘭金(Rankin)循環中產生額外的動力)。然而，沒有商業可得的燃氣渦輪可在該循環中操作且需要製造高純度氧的動力，明顯降低方法的總效率。一些研究已比較這些方法並顯示每一方法的一些優點。參見例如BOLLAND,OLAV,and UNDRUM,HENRIETTE,Removal of CO 2 from Gas Turbine Power Plants: Evaluation of pre-and post-combustion methods，SINTEF Group，見http://www.energy.sintef.no/publ/xergi/98/3/3art-8-engelsk.htm(1998)。
其他降低CO2排放的方法包括化學計量的排氣循環，例如天然氣複合循環(NGCC)。在習用的NGCC系統中，提供足夠的燃料化學計量燃燒僅需要約40%的空氣進入體積，而剩餘60%的空氣體積係作為緩和溫度及冷卻煙道氣，使適合導入後續的膨脹機，但也不利地產生難以去除的過剩氧氣副產物。一般的NGCC產生低壓煙道氣，需要將所產生的一部份動力抽取CO2以隔離或EOR，因而降低NGCC的熱效率。而且，抽取CO2的設備大且昂貴，且需要一些壓縮階段以使常壓氣體達EOR或隔離所需的壓力。該限制為與例如煤的其他化石燃料之燃燒有關的低壓煙道氣之後燃燒碳捕捉的典型。
於是，對於低排放、高效率動力產生及CO2捕捉或製造方法仍有實質的需要。
本揭示目標為三循環動力產生系統及操作該系統的方法。在一示範性系統中，整合的系統包含燃氣渦輪系統、排氣循環系統及氣體膨脹機。該燃氣渦輪系統具有第一燃燒室，係配置以在經壓縮的循環流存在之下，將第一經壓縮的氧化劑及第一燃料化學計量地燃燒。該燃燒室將第一排放流導至膨脹機，以產生氣態排氣流且至少部分地驅動主要壓縮機。排氣循環系統接收來自燃氣渦輪系統膨脹機的氣態排氣流，並以其中所含的熱能製造動力，例如經由熱回收蒸汽產生單元。排氣循環系統進一步將排氣流導至主要壓縮機，在此將排氣流壓縮以產生經壓縮的循環流。將經壓縮的循環流導至燃燒室，作為配置以緩和第一排放流溫度的稀釋劑。該整合系統進一步包括經由沖刷流與經壓縮的循環流以流體連接的CO2分離器。該CO2分離器由沖刷流產生富CO2流及包含富氮氣體的殘餘流。如上述，該整合系統也包括氣體膨脹機。氣體膨脹機經由殘餘流以流體連接至CO2分離器，用以將殘餘流膨脹而產生動力。
在操作三循環動力產生系統的示範性方法中，產生動力的方法可包含在第一燃燒室中及在經壓縮的循環流存在之下，將第一經壓縮的氧化劑及第一燃料化學計量地燃燒。燃燒可因而產生第一排放流。經壓縮的循環流可作為配置以緩和第一排放流溫度的稀釋劑。該方法進一步包括將膨脹機中的第一排放流膨脹至至少部分驅動第一壓縮機並產生氣態排氣流。第一排放流的膨脹可產生供其他用途的額外動力。該方法進一步包括將氣態排氣流導至第一壓縮機，其中該第一壓縮機將氣態排氣流壓縮並藉以產生經壓縮的循環流。更進一步，該方法包括經由沖刷流將一部份經壓縮的循環流抽取至CO2分離器，該CO2分離器係經由衍生自CO2分離器且主要以富氮氣體所組成之殘餘流以流體連接至氣體膨脹機。示範性方法進一步包括在氣體膨脹機中將殘餘流膨脹，以產生機械動力及排氣。
在以下詳細說明的單元中，以較佳的具體實例結合說明本揭示的特定具體實例。然而，在一定程度上，以下說明係針對本揭示的特殊具體實例或特殊用途，係僅要作為示範目的及簡單地提供示範的具體實例之說明。因此，本揭示並不受限於下述的特定具體實例，而是包括所有落在隨附之申請專利範圍之真正精神及範圍內的替代方案、修改、及均等者。
在此所用的各種詞語定義如下。在一定程度上，以下未定義而使用於本申請專利範圍內的詞語，應給予以相關技藝者在至少一印刷的出版品或提出的專利中呈現的詞語所給予的最寬廣定義。
如在此所用，詞語「天然氣」係指自原油井(相關的氣體)或自次岩層的含氣層(非相關的氣體)所得的多重成份氣體。天然氣的組成及壓力可有很明顯的變化。一般天然氣流含有的甲烷(CH4)為主要成份，亦即大於天然氣流的50莫耳%為甲烷。天然氣流也可含有乙烷(C2H6)、較高分子量的烴(例如C3-C20烴)、一種或多種酸氣體(例如硫化氫、二氧化碳)、或其任意組合。天然氣也可含有少量的污染物，例如水、氮、硫化鐵、蠟、原油、或其任意組合。
如在此所用，詞語「化學計量燃燒」係指包含一定量之含有燃料及氧化劑的反應物及一體積之定量之因反應物的燃燒所形成的產物之燃燒反應，其中反應物的全部量皆用以形成產物。如在此所用，詞語「實質上為化學計量燃燒」係指燃燒的燃料對氧的莫耳比約為化學計量比所需氧之約±10%，或更佳為化學計量比所需氧之約±5%範圍之燃燒反應。例如，就甲烷而言，燃料對氧的化學計量比為1:2(CH4+2O2>CO2+2H2O)。就丙烷而言，燃料對氧的化學計量比為1:5。測量實質上為化學計量燃燒的另一方法為所供應的氧對化學計量燃燒所需氧的比例，例如自約0.9:1至約1.1:1，或更佳為自約0.95:1至約1.05:1。
如在此所用，詞語「流(或物流)」係指一定量流體，雖然詞語“流(或物流)”的使用一般意為移動量流體(例如具有速度或質量流率)。然而，詞語「流(或物流)」不需速度、質量流率、或圍住該流(或物流)的特殊管道類型。
在此揭示的系統及方法的具體實例可用以製造超低排放的電力及加強油回收(EOR)或隔離應用的CO2。如在此揭示的具體實例，空氣及燃料的混合物可以化學計量地燃燒，且同時與循環的排氣流混合。通常包含例如CO2之燃燒產物的循環排氣流可使用作為稀釋劑，以控制或緩和化學計量燃燒與進入後續膨脹機的煙道氣之溫度。
為了消除過剩氧的去除成本，在接近化學計量條件的燃燒(或「略富含」的燃燒)可證明為有利的。將煙道氣冷卻及將水自物流冷凝出，可製造相當高含量的CO2物流。而一部份的循環排氣可用於密閉的布雷頓循環中的溫度緩和，剩餘的沖刷流可用於EOR應用，及可在微量或無SOx、NOx或CO2排放至大氣之下製造電力。例如，如在此所揭示的具體實例，可在用以排放富氮氣體的CO2分離器中處理沖刷流，隨後可將該富氮氣體在氣體膨脹機中膨脹，以產生額外的機械動力。在此揭示的系統結果為於三個分離的循環中的動力製造，及在更經濟有效水準下製造或捕捉額外的CO2。在一些執行例中，可經由各種裝置將富氮排放流加熱，以增加用氮氣流之膨脹機所獲得的動力。另外，在一些執行例中，可將在膨脹機後的氮排氣冷卻，並用以提供冷凍，其可用以增進布雷頓循環中的壓縮機及/或排氣循環的效率。也可將冷的氮氣流使用於增進方法效率的其他應用。
或是，可將經排放的富氮氣體送至EOR設施供額外的壓縮及/或注入井中供油回收及/或壓力維持。雖然可能完全獨立地製造供貯油層壓力維持的氮氣及供EOR的CO2，當在整合方法中製造氮氣及CO2二者時，在此揭示的具體實例也可利用此可能的協同作用，在更低成本且也製造動力之下，完成這些氣體的製造。
現在參考圖形，圖1描述使用複合循環配置而配置以提供增進的後燃燒CO2捕捉方法之動力產生系統100。在至少一個具體實例中，動力產生系統100可包括燃氣渦輪系統102，其特徵為密閉的布雷頓循環。在一具體實例中，燃氣渦輪系統102可具有第一或主要壓縮機104，而其經由常見的柄108或其他機械、電力、或其他動力連接與膨脹機106連接，藉以使膨脹機106所產生的部分機械能驅動壓縮機104。膨脹機106可產生也供其他用途的動力。燃氣渦輪系統102可為標準的燃氣渦輪，而主要壓縮機104及膨脹機106分別形成標準燃氣渦輪的壓縮機及膨脹機的末端。然而，在其他具體實例中，主要壓縮機104及膨脹機106可為系統102的個別化組件。
燃氣渦輪系統102也可包括燃燒室110，而其經配置以將與經壓縮的氧化劑114混合的燃料流112燃燒。在一個或多個具體實例中，燃料流112可包括任何適用的烴氣體或液體，例如天然氣、甲烷、乙烷、石油腦、丁烷、丙烷、合成氣、柴油、煤油、航空燃料、煤衍生的燃料、生質燃料、加氧烴原料、或其組合。經壓縮的氧化劑114可衍生自與燃燒室110以流體連接的第二或入口壓縮機118，並用以將進料氧化劑120壓縮。在一個或多個具體實例中，進料氧化劑120可包括任何含氧的適用氣體，例如空氣、富氧空氣、貧氧空氣、純氧、或其組合。
以下將更詳細說明，燃燒室110也可接收經壓縮的循環流144，其包括主要含有CO2及氮成份的煙道氣。經壓縮的循環流144可衍生自主要壓縮機104，並用以幫助促進經壓縮的氧化劑114及燃料112之化學計量燃燒，且也增加操作流體中的CO2濃度。在經壓縮的循環流144的存在下，導向膨脹機106入口的排放流116係燃料流112及經壓縮的氧化劑114的燃燒產物。在至少一個具體實例中，燃料流112可主要為天然氣，藉以產生排放流116，而其包括汽化的水、CO2、氮、氮氧化物(NOx)、及硫氧化物(SOx)之體積部分。在一些具體實例中，因為燃燒平衡的限制，少部分未燃燒的燃料112或其他化合物也可存在於排放流116中。當排放流116通過膨脹機106而膨脹時，其產生機械動力以驅動主要壓縮機104、發電機、或其他設施，並也製造具有更高CO2含量的氣態排氣流122。
動力產生系統100也可包括排氣循環(EGR)系統124。雖然圖中描述的EGR系統124含有許多設備，所述的圖僅為代表性，且可使用將排氣循環122循環回到主要壓縮機的任何系統。在一個或多個具體實例中，EGR系統124可包括熱回收蒸汽產生器(HRSG)126、或類似裝置，以流體連接至蒸汽燃氣渦輪128。在至少一個具體實例中，HRSG 126及蒸汽燃氣渦輪128的組合特徵為密閉的蘭金循環。當與燃氣渦輪系統102組合時，HRSG 126及蒸汽燃氣渦輪128可形成複合循環動力產生廠的一部份，例如天然氣的複合循環(NGCC)廠。可將氣態排氣流122送至HRSG 126，以產生蒸汽130及經冷卻的排氣132之物流。在一些具體實例中，可將蒸汽130送至蒸汽燃氣渦輪128，以產生額外的電力。
圖1描述EGR系統124中的額外設備，視需要可納入一些執行例中。可將經冷卻的排氣132送至配置以降低經冷卻的排氣132的溫度及產生經冷卻的循環氣流140之至少一個冷卻單元134。在一個或多個具體實例中，冷卻單元134可為直接接觸的冷卻器、蛇行管冷卻器、機械冷凍單元、或其組合。也可將冷卻單元134配置為經由水漏失流138而去除部分的冷凝水，在至少一個具體實例中，經由管線141將其導至HRSC 126，以提供產生額外的蒸汽130之水源。在一個或多個具體實例中，可將經冷卻的循環氣流140導至與冷卻單元134為流體連接的增壓壓縮機142(若需要)。在冷卻單元134中將經冷卻的排氣132冷卻，可降低在增壓壓縮機142中將經冷卻的循環氣流140壓縮所需的動力，或消除其對能量的整體需求。
可將增壓壓縮機142配置以在將經冷卻的循環氣流140導入主要壓縮機104之前，增加其壓力。與習用的風扇或鼓風機系統相反，增壓壓縮機142增加經冷卻的循環氣流140的整體密度，藉以將相同體積流以增加的質量流率導至主要壓縮機104。因為主要壓縮機104一般受體積流所限制，經由主要壓縮機104導入更多的質量流可導致主要壓縮機104更高的排放壓力，藉以通過膨脹機106轉化為更高的壓力比。通過膨脹機106產生更高的壓力比可容許更高的入口溫度，所以增加膨脹機106的動力及效率。此可證明是有利的，因為富CO2的排放流116通常維持較高的比熱容量。於是，當使用冷卻單元134及增壓壓縮機142時，其每一者可用以使燃氣渦輪系統102的操作最佳化或改良。
可將主要壓縮機104配置以將接收自例如增壓壓縮機142的EGR系統124之經冷卻的循環氣流140壓縮至表稱壓力高於燃燒室110的壓力，藉以產生經壓縮的循環流144。在至少一個具體實例中，沖刷流146可自經壓縮的循環流144排出，且隨後在CO2分離器148中處理，經由管線150捕捉於高壓下的CO2。管線150中經分離的CO2可用於銷售、使用於其他需要二氧化碳的方法、及/或將其壓縮並注入加強油回收(EOR)的陸上貯油層、隔離、或其他目的。
基本上已缺乏CO2且主要由氮所組成的殘餘流151可衍生自CO2分離器148。在一個或多個具體實例中，殘餘流151可在與CO2分離器148以流體連接的氣體膨脹機152中膨脹，例如動力製造用之氮膨脹機。如圖1-3所描述，氣體膨脹機152可視需要經由常見的柄154或其他機械、電動、或其他動力連接與入口壓縮機118連接，藉以使氣體膨脹機152所產生的部分動力驅動入口壓縮機118。在氣體膨脹機152中膨脹之後，主要由氮所組成的排氣156可排放至大氣或執行技藝中已知的其他下游應用。例如，經膨脹的氮流可使用於蒸發的冷卻方法中，其配置以進一步降低排氣的溫度，如同時申請的美國專利申請案標題為「以排氣循環及直接接觸冷卻器之化學計量燃燒」中之一般性描述，其內容以一致的方式納入本文。在至少一個具體實例中，氣體膨脹機152、入口壓縮機118、及CO2分離器的組合特徵為開放的布雷頓循環、或系統100的第三動力製造組件。
將氣體膨脹機152及入口壓縮機118組合或連接可組成開放的布雷頓循環，不論與入口壓縮機118連接或不連接，氣體膨脹機152提供系統100的第三動力製造組件。例如，氣體膨脹機152可用以對其他應用提供動力，且不直接與化學計量的壓縮機118連接。例如，在以膨脹機152產生的動力與壓縮機118的需求之間可能有實質的不相符合。在此情況下，可使用膨脹機152以驅動需要較低動力之較小的壓縮機(未示出)(或驅動入口壓縮機118及一個或多個額外的設施)。
而在其他具體實例中，也將參考圖8在以下討論，可用下游的壓縮機188取代氣體膨脹機152，壓縮機188係配置以將殘餘流151壓縮且產生適合注入壓力維持的貯油層或EOR應用之經壓縮的排氣190。
如在此所述的EGR系統124，可進行以達到動力產生系統100的操作流體中較高濃度的CO2，藉以使後續的隔離、壓力維持、或EOR應用之更有效的CO2分離。例如，在此揭示的具體實例可有效地增加煙道氣排氣流中的CO2濃度至約10體積%或更高。為完成此事，燃燒室110可用以將燃料112與經壓縮的氧化劑114之入流混合物加以化學計量地燃燒。為緩和化學計量燃燒的溫度以符合膨脹機106入口溫度及組件的冷卻需求，衍生自經壓縮的循環流144的一部份排氣可注入燃燒室110中，作為稀釋劑。因此，本揭示的具體實例基本上可消除操作流體中任何過剩的氧，而同時增加其CO2的組成。如此，氣態排氣流122可具有低於約3.0體積%的氧，或低於約1.0體積%的氧，或低於約0.1體積%的氧，或甚至低於約0.001體積%的氧。在一些執行例中，燃燒室110或更特別是至燃燒室的入口流可被控制較佳至化學計量燃燒，以進一步降低氣態排氣流122的氧含量。
現在將討論系統100的示範操作特性。應可體會在此揭示的任何具體實例的各種組件中所達到或遭遇的特定溫度及壓力，可視使用的氧化劑純度及膨脹機、壓縮機、冷卻器等的特定製造及/或樣式的其他因子而改變。因此，應體會在此所述的特殊數據係僅為說明的目的，且不應被理解為彼之唯一解釋。例如，在此所述之具體實例中，入口壓縮機118可配置以作為化學計量壓縮機，提供經壓縮的氧化劑114壓力介於約280 psia及約300 psia的範圍。然而，在此也考慮空氣衍生的燃氣渦輪技術，其可製造及消耗壓力達約750 psia及更高。
主要壓縮機104可配置以將經循環的排氣循環及壓縮至表稱壓力高於或處於燃燒室110的壓力之經壓縮的循環流144中，且在燃燒室110中使用一部份該經循環的排氣作為稀釋劑。因為燃燒室110中所需稀釋劑的量可視用以化學計量燃燒的氧化劑純度或膨脹機106的樣式而定，熱偶環及/或氧感應器(未示出)可與燃燒室及/或膨脹機結合。例如，熱偶及/或氧感應器可配置在燃燒室110的出口、在膨脹機106的入口、及/或在膨脹機106的出口。在操作時，熱偶及感應器可用以測定一種或多種物流的組成及/或溫度，而該物流用於決定作為稀釋劑所需的排氣體積，以將燃燒產物冷卻至所需的膨脹機入口溫度。另外或是，熱偶及感應器可用以決定注入燃燒室110之氧化劑的量。因此，當回應以熱偶偵測的熱需求及以氧感應器偵測的氧濃度時，可操作或控制經壓縮的循環流144及/或經壓縮的氧化劑114之體積質量流，以符合需求。可透過任何適當的流量控制系統，控制體積質量流率。
在至少一個具體實例中，在化學計量燃燒時，橫跨燃燒室110可遭遇約12-13 psia的壓降。燃料112及經壓縮的氧化劑114之燃燒可產生介於約2000℉及約3000℉的溫度與壓力範圍為250 psia至約300 psia。因為增加的質量流及衍生自經壓縮的循環流144之富CO2操作流體的較高比熱容量，橫跨膨脹機106可達到較高的壓力比，因而容許較高的入口溫度及增加膨脹機106的動力。
自膨脹機106離開的氣態排氣流122可處於大氣或接近大氣的壓力。在至少一個具體實例中，氣態排氣流122可具有壓力為約15.2 psia。氣態排氣流122在通過HRSG 126之前的溫度可在約1180℉至約1250℉的範圍，以產生管線130中的蒸汽及冷卻的排氣132。經冷卻的排氣132可在約190℉至約200℉的溫度範圍。在一個或多個具體實例中，冷卻單元134可降低經冷卻的排氣132之溫度，藉以產生溫度介於約32℉及120℉之經冷卻的循環氣流140，主要視在特定位置及特定季節的濕球溫度而定。
如一個或多個具體實例，增壓壓縮機142可配置以提高經冷卻的循環氣流140的壓力至約17.1 psia至約21 psia的壓力範圍。結果，主要壓縮機104將具有更高密度及增加的質量流之經循環的煙道氣工作流體接收及壓縮，如此可以容許實質上更高的排放壓力，且同時維持相同或類似的壓力比。在至少一個具體實例中，排放自主要壓縮機104之經壓縮的循環流144的溫度可為約800℉，壓力約為280 psia。
下表提供以複合循環燃氣渦輪為基礎的測試結果及成效估計，並描述有及無增壓壓縮機142增加的好處。
由表1可明顯看出，包括增壓壓縮機142的具體實例因為增加壓力比，可導致增加膨脹機106的動力(亦即「燃氣渦輪膨脹機動力」)。雖然可增加主要壓縮機104的動力需求，但是其增加的動力可為膨脹機106動力輸出的增加所補償，因而導致整體熱力學成效效率增進約1% lhv(低位熱值)。
而且，加入增壓壓縮機142也可增加氮膨脹機152的動力輸出及沖刷流146管線中的CO2沖刷壓力。當增壓壓縮機142可增加氮膨脹機152的動力輸出時，由表1可看到氮膨脹機152為對具有或不具有增壓壓縮機的整體系統100之效率的重要貢獻者。
因為較高的CO2分壓，增加沖刷流146的沖刷壓力可導致CO2分離器148中增進的溶劑處理成效。該增進可包括、但非限於以溶劑萃取方法的縮小設備尺寸的形式之整體資本支出的降低。
現在參考圖2，以圖1的動力產系統100的替代具體實例說明，以系統200作為示範及說明。如此，參考圖1可最瞭解圖2。與圖1的系統100相似，圖2的系統200包括與排氣循環(EGR)系統124連接或以其支援的燃氣渦輪系統102。然而，圖2中的EGR系統124可包括一具體實例，其中增壓壓縮機142接著HRSG 126或與其以流體連接。如此，經冷卻的排氣132可在冷卻單元134中降低溫度之前於增壓壓縮機142中被壓縮。因此，冷卻單元134可作為用以去除因增壓壓縮機142產生的壓縮熱的後冷卻器。如先前揭示的具體實例，水漏失流138可以或不導至HRSG 126，以產生額外的蒸汽130。
如上述討論，然後可將經冷卻的循環氣流140導至將其進一步壓縮的主要壓縮機104，藉以產生經壓縮的循環流144。應可體會，將經冷卻的排氣132於增壓壓縮機142中壓縮後於冷卻單元134中冷卻，可降低將經冷卻的循環氣流140壓縮至後續主要壓縮機104中預定的壓力所需之動力量。
圖3說明圖1低排放動力產生系統100的另一具體實例，以系統300為例。如此，參考圖1及2可最瞭解圖3。與分別說明於圖1及圖2的系統100、200相似，系統300包括以EGR系統124支援或與其連接的燃氣渦輪系統102。然而，圖3中的EGR系統124可包括第一冷卻單元134及第二冷卻單元136，具有在其之間以流體連接的增壓壓縮機142。如前述的具體實例，每一冷卻單元134、136可為本技藝中已知的直接接觸冷卻器、蛇行管冷卻器、或類似者。
在一個或多個具體實例中，可將排放自HRSG 126之經冷卻的排氣132送至第一冷卻單元134，以製造冷凝的水漏失流138及經冷卻的循環氣流140。可將經冷卻的循環氣流140導向增壓壓縮機142，以對經冷卻的循環氣流140增加壓力，且然後將其導至第二冷卻單元136。第二冷卻單元136可作為用以將增壓壓縮機142所產生的壓縮熱去除的後冷卻器，且經由水漏失流143也去除另外的冷凝水。在一個或多個具體實例中，每一水漏失流138、143可以或不導至HRSG 126，以產生額外的蒸汽130。
然後可將經冷卻的循環氣流140導入主要壓縮機104，以產生高於或處於燃燒室110的表稱壓力之經壓縮的循環流144。應可體會，將經冷卻的排氣132於第一冷卻單元134中冷卻，可降低將經冷卻的循環氣流140在增壓壓縮機142中壓縮所需之動力量。而且，在第二冷卻單元136中進一步將排氣冷卻，可降低將經冷卻的循環氣流140壓縮至後續主要壓縮機104中預定的壓力所需之動力量。
現在參考圖4，描述低排放動力產生系統400的另一具體實例，與圖3的系統300之一些觀點類似。如此，參考圖1及3，可最瞭解圖4的系統400。然而應注意的是，參考圖1-3所揭示的個別具體實例或其組合可在不偏離本揭示的範圍內，進行及/或省略與圖4的系統400之關聯。例如，EGR系統124所使用的特定設施及設備可依本文任何處所述者加以變化。
如上述，排放自主要壓縮機104之經壓縮的循環流144的溫度可為約800℉，並表現壓力約為280 psia。結果，自經壓縮的循環流144排出的沖刷流146可表現類似的溫度及壓力。應再次注意的是特定溫度及壓力將無可避免地隨膨脹機、壓縮機、冷卻器等的特定的製造及樣式而改變。因為壓力遠高於以後燃燒CO2回收之習用的天然氣複合循環(NGCC)系統，促使在CO2分離器148中使用低能量-強烈的氣體處理方法。例如，該高溫及高壓與得自燃燒室110中採用的化學計量燃燒之實質上缺乏氧而結合時，可容許使用熱的碳酸鉀溶劑，以抽取沖刷流146的CO2。在另一具體實例中，CO2選擇性吸附劑可包括但不限於單乙醇胺(“MEA”)、二乙醇胺(“DEA”)、三乙醇胺(“TEA”)、碳酸鉀、甲基二乙醇胺(“MDEA”)、活化的甲基二乙醇胺(“aMDEA”)、二甘醇胺(“DGA”)、二異丙醇胺(“DIPA”)、哌嗪(“PZ”)、其衍生物、其混合物、或其任意組合。其他適合的吸附劑及技術可包括但不限於碳酸丙烯酯之物理性吸附劑溶劑、以及其他碳酸烷酯、二至十二個乙二醇單元的聚乙二醇之二甲醚(SelexolTM方法)、N-甲基-吡咯烷酮、環丁碸、及使用氣體處理方法。
在一具體實例中，CO2分離器148中的氣體處理方法可能需要將沖刷流146的溫度冷卻至約250℉-300℉。為達如此，可經由例如與殘餘流151以流體連接的反向交換熱交換器之熱交換器158傳送沖刷流146。在至少一個具體實例中，自CO2分離器148中的沖刷流146抽取CO2，可使富氮殘餘流151處於或接近沖刷流146的高壓及於約150℉的溫度。在一具體實例中，可經由熱交換器158抽取與將沖刷流146冷卻相關的熱能，且用以對殘餘流151再加熱，藉以產生溫度約750℉及壓力約270-280 psia的熱氮蒸汽160。以沖刷流146的熱交換為加熱殘餘流的一種方式，其他方法在本揭示的範圍內。例如，在一個或多個具體實例中，可使用HRSG 126進行物流151的補充加熱，以提供熱以及產生蒸汽130。在此描述其他示範性方法，且不應視為將殘餘流151加熱的可行方法完全列出。
在一個或多個具體實例中，然後可經由氣體膨脹機152將熱氮蒸汽160膨脹。於是，在熱交換器158中反向交換的熱可配置以捕捉衍生自主要壓縮機104之實質量的壓縮能，並使用其將抽取自氣體膨脹機152的動力最大化，且視需要驅動化學計量入口壓縮機118。在至少一個具體實例中，主要以大氣壓的氮所組成之排氣156可無害地排放至大氣，或在技藝中已知的其他下游應用中進行。例如蒸發冷卻的方法之示範性下游應用描述於同時提出之如上述的美國專利申請案標題為「以排氣循環及直接接觸冷卻器之化學計量燃燒」。
在系統400啟動及正常操作時，當氣體膨脹機152可能無法供應操作入口壓縮機118所有需要的動力時，至少一個馬達162、例如電動馬達，可與氣體膨脹機152協同使用。例如，可依需要設計馬達162的尺寸，使在系統400正常操作時，可配置馬達162以提供氣體膨脹機152短暫落差的動力。另外或是，可能有時在操作時，氣體膨脹機152會製造比入口壓縮機118所需更多的能量。在一些執行例中，至少一個馬達162可為馬達/發電機系統，可選擇性配置以提供動力例如由電網，提供動力至壓縮機，或由渦輪152所產生的動力而產生電力。
參考圖5，描述低排放動力產生系統500的另一具體實例，與圖4的系統400的一些觀點類似。因此，不再詳細描述圖5的整個系統500，但參考圖1、3及4可最瞭解。應注意的是，參考圖1-4所揭示的任何具體實例可在不偏離本揭示的範圍內，於系統500中分別或組合執行。
在一具體實例中，當沖刷流146自經壓縮的循環流144排出時，其溫度可因催化設備164所使用的催化方法而增加。在操作時，可配置催化設備164以降低沖刷流中氧及/或一氧化碳含量，並將其轉化成殘餘的CO2及熱。催化設備164可為單一裝置，或為平行、序列、或平行及序列組合的多個裝置。在一具體實例中，催化設備164可為僅需要少量動力以操作的小型裝置。示範性催化設備164可包括一般使用於HRSG以符合排放需求的氧還原催化劑。該系統通常非設計用以去除大量的氧，但若在經壓縮的循環流144中殘留明顯量的氧時，沖刷流146在進一步處理或使用之前，例如壓縮及加強油回收(EOR)的注入、CO2分離等，可不止一次循環通過催化設備164。
而且，在沖刷流146中任何的殘留烴也可在催化設備164中燃燒。在至少一個具體實例中，因存在於沖刷流146中約1200 ppm的氧之完全催化轉化，沖刷流146的溫度可自約785℉增加至約825℉。可用於催化設備164的示意催化劑可包括、但不限於鎳、鉑、銠、釕、鈀、或彼之衍生物、彼之混合物、彼之任意組合。此增加的熱含量可導入熱交換器158，並與富氮殘餘流151反向交換，藉以產生較高溫的熱氮蒸汽160，及促使氣體膨脹機152中更有效及有力的膨脹方法。
在一個或多個具體實例中，對包括氣體膨脹機152之三循環系統更進一步的增強，可經由管線166將水注入熱氮蒸汽160，以增加氣體膨脹機152的質量輸出且結果增加產生的動力。該水可為經處理的霧化水或蒸汽。在至少一個具體實例中，因注入霧化水或蒸汽所提供的補充動力可增加約169 MW至約181 MW的動力輸出。應可體會動力輸出通常會隨氣體膨脹機的製造及樣式而定。應注意的是，經由管線166將霧化水或蒸汽注入熱氮蒸汽160以增加通過氣體膨脹機152的質量流，可在不偏離本揭示的範圍內，於本文揭示的任何具體實例中執行。
參考圖6，描述低排放動力產生系統600的另一具體實例，與圖5的系統500類似。因此，不再詳細描述整個系統600，但參考圖5可最瞭解。在一具體實例中，系統600可包括配置在氣體膨脹機152之前之額外的化學計量燃燒室168。燃燒室168可配置以將燃料170及經壓縮的氧化劑172的組合物化學計量燃燒，很像上述的燃燒室110，以在高溫及高壓下產生排放流174。在一具體實例中，燃料170及經壓縮的氧化劑172可分別衍生自與燃料112及經壓縮的氧化劑114相同的來源，而燃料112和經壓縮的氧化劑114係輸送進第一燃燒室110。在含有額外燃燒室168的執行例中，熱交換器158可通過其他裝置將沖刷流冷卻，例如將系統600或其他處之一個或多個其他物流加熱。例如，在沖刷流上的熱交換器可對HRSG或對重組方法提供額外的熱。
在其他具體實例中，特別是希望或需要零CO2排放的具體實例中，燃料170可主要以氫所組成。在至少一個具體實例中，以HRSG 126或分離的HRSG(未示出)將甲烷重組，可製造氫燃料。在甲烷的重組及水氣的移動之後，以吸收塔(未示出)可去除氫產物流中的CO2，例如以CO2分離器148。然後在燃燒室168內將氫與熱氮蒸汽160流中的一些氮摻合，以製造可接受的燃氣渦輪燃料。
排放自熱交換器158或排放自CO2分離器148的熱氮蒸汽160可作為配置以緩和燃燒及排放流174之溫度的稀釋劑。在至少一個具體實例中，離開燃燒室168的排放流174在氣體膨脹機中膨脹以產生機械動力之前，可具有溫度約2500℉。應可體會，氣體膨脹機152、燃燒室168、及入口壓縮機118的組合之特徵在於分離的標準燃氣渦輪系統，其中入口壓縮機118成為壓縮機的末端，且氣體膨脹機152成為燃氣渦輪的膨脹機末端。
在一個或多個具體實例中，排氣156可具有溫度約1100℉。在至少一個具體實例中，可將排氣156導至HRSG 126以回收熱，作為蒸汽燃氣渦輪128的動力。在其他具體實例中，可將排氣156導至外部HRSG及蒸汽燃氣渦輪(未示出)，以產生供其他應用的動力。在任何情況下，可將富氮殘餘流151以在此所討論的任何方式加以配置，例如在通過膨脹機152之後，經由氮排氣、經由隔離、EOR、或壓力維持的操作等。
現在參考圖7，描述低排放動力產生系統700的另一具體實例，與圖6的系統600類似。因此，不再詳細描述圖7的整個系統700，但參考圖6及其後的說明可最瞭解。不使用分離的入口壓縮機118及氮膨脹機152(見圖1-6)，圖7中所描述的系統700可包括第二燃氣渦輪系統702，其具有第二壓縮機176及第二膨脹機178。在一個或多個具體實例中，第二壓縮機176可接收並壓縮第二進料氧化劑180。與上述圖1-6所示的進料氧化劑120類似，第二進料氧化劑180可包括含有氧之任何適當的氣體，例如空氣、富氧空氣、或彼之組合。可將第二壓縮機176配置以壓縮第二進料氧化劑180及產生第二經壓縮的氧化劑182。如所述，可由第二經壓縮的氧化劑182流供給或抽取燃燒室110所需之經壓縮的氧化劑114，且作為如一般上述中的相同功能。
在操作時，可配置燃燒室168以化學計量地燃燒燃料170及第二經壓縮的氧化劑182的組合物，以產生高溫及高壓的排放流174。在一個或多個具體實例中，來自熱交換器158的氮蒸汽160或來自CO2分離器148的殘餘流可作為稀釋劑，係配置以緩和第二燃燒室168中的燃燒溫度。在一具體實例中，燃料170可衍生自與輸送進入第一燃燒室110之燃料112相同的來源，例如烴燃料。在其他具體實例中，當希望或需要零CO2排放時，燃料170可主要由氫所組成，如參考圖6之一般上述。
若是使用烴燃料，便自然會產生CO2排放。然而，因為使用大量純氮流作為稀釋劑，所得的CO2排放會明顯比習用的NGCC發電廠更少。例如，在一具體實例中，得自系統700的CO2排放僅約80 lbs/MWhr，相較於習用的NGCC發電廠約為400 lbs/MWhr。在一個或多個具體實例中，來自第二膨脹機178的排氣156可具有溫度約1100℉。在至少一個具體實例中，可將排氣156導至第二HRSG 184以回收熱，作為分開的蒸汽燃氣渦輪186中的動力。然而，在另一具體實例中，可將排氣156導至第一HRSG 126以回收熱，作為蒸汽燃氣渦輪128中的動力。再次可瞭解排氣156於通過第二HRSG 184之後，可排放或使用於如上述的烴回收操作(未示出)。
應可體會，圖7的系統700可容許使用商業可得的燃氣渦輪，而非接受耗費的升級品以獲得客製的空氣壓縮機及客製的膨脹機。因為第二膨脹機178的入口溫度可達到溫度約2500℉，系統700也可在更高效率下製造更多的淨動力。
現在參考圖8，描述低排放動力產生系統800的另一具體實例，與圖3的系統300類似。因此，不再詳細描述圖8的整個系統800，但參考圖1及3可最瞭解。然而應注意的是，在不偏離本揭示的範圍內，參考圖1-6所揭示的具體實例可個別或與圖8的系統800組合而執行。在一示範性具體實例中，主要由衍生自CO2分離器148的氮所組成的殘餘流151可傳送至下游的壓縮機188。可配置下游壓縮機188將殘餘流151壓縮，且產生具有壓力例如為約3400 psi或壓力適合注入壓力維持應用的貯油層之經壓縮的排氣190。
以下游的壓縮機188將殘餘流151壓縮，在通常將甲烷氣體重新注入烴井以維持井壓力的應用證明為有利的。如在此揭示的具體實例，反而可將氮注入烴井，而殘餘的甲烷氣體可販售或使用作為相關應用的燃料，例如提供用於燃料流112、170的燃料(見圖6及7)。
繼續參考圖5-7，下表提供以無膨脹循環的系統(例如圖8的系統800)、燃燒室168中無額外燃燒的系統(例如圖5的系統500)、及燃燒室168中有額外燃燒的系統(例如分別為圖6及7的系統600、700)為基礎之測試結果及成效估計。該數據反映燃燒甲烷燃料170以供燃燒。
由表2應很明顯，在燃燒室168中具有燃燒的具體實例可導致明顯較高的複合循環動力輸出，當與燃燒室168中不進行燃燒的具體實例相比幾乎為雙倍的動力輸出。而且，如在此揭示使用燃燒的系統之整體熱力學成效效率相對於不執行該燃燒技術的具體實例，表現出實質的提升或增進約3.3% lhv(低位熱值)。
本揭示可接受各種修改及替代形式，以上討論的示範性具體實例僅以實例的方式顯示。然而，應再次瞭解本揭示並非限於在此揭示的特殊具體實例。事實上，本揭示包括所有落在隨附之申請專利範圍之真正精神及範圍內的替代方案、修改、及均等者。
100．．．動力產生系統
102．．．燃氣渦輪系統
104．．．主要壓縮機
106．．．膨脹機
108．．．柄
110．．．燃燒室
112．．．燃料流
114．．．經壓縮的氧化劑
116．．．排放流
118．．．入口壓縮機
120．．．進料氧化劑
122．．．氣態排氣流
124．．．排氣循環系統
126．．．熱回收蒸汽產生器
128．．．蒸汽燃氣渦輪
130．．．蒸汽
132．．．排氣
134．．．冷卻單元
136．．．第二冷卻單元
138．．．水漏失流
140．．．經冷卻的循環氣流
141．．．管線
142．．．增壓壓縮機
143．．．水漏失流
144．．．經壓縮的循環流
146．．．沖刷流
148．．．CO2分離器
150．．．管線
151．．．殘餘流
152．．．氣體膨脹機
154．．．柄
156．．．排氣
158．．．熱交換器
160．．．熱氮蒸汽
162．．．馬達
164．．．催化設備
166．．．管線
168．．．燃燒室
170．．．燃料
172．．．經壓縮的氧化劑
174．．．排放流
176．．．第二壓縮機
178．．．第二膨脹機
180．．．第二進料氧化劑
182．．．第二經壓縮的氧化劑
184．．．第二HRSG
188．．．下游壓縮機
200．．．系統
300．．．系統
400．．．系統
500．．．系統
600．．．系統
700．．．系統
702．．．第二燃氣渦輪系統
800．．．系統
當審視本文的詳細說明及具體實例的非限制用實例的圖式，明顯呈現本揭示的前述及其他優點，其中：
圖1說明根據本揭示之一個或多個具體實例的低排放動力產生及加強CO2回收之整合系統。
圖2說明根據本揭示之一個或多個具體實例的另一低排放動力產生及加強CO2回收之整合系統。
圖3說明根據本揭示之一個或多個具體實例的另一低排放動力產生及加強CO2回收之整合系統。
圖4說明根據本揭示之一個或多個具體實例的另一低排放動力產生及加強CO2回收之整合系統。
圖5說明根據如本揭示之一個或多個具體實例的另一低排放動力產生及加強CO2回收之整合系統。
圖6說明根據如本揭示之一個或多個具體實例的另一低排放動力產生及加強CO2回收之整合系統。
圖7說明根據如本揭示之一個或多個具體實例的另一低排放動力產生及加強CO2回收之整合系統。
圖8說明根據如本揭示之一個或多個具體實例的另一低排放動力產生及加強CO2回收之整合系統。
100．．．動力產生系統
102．．．燃氣渦輪系統
104．．．主要壓縮機
106．．．膨脹機
108．．．柄
110．．．燃燒室
112．．．燃料流
114．．．經壓縮的氧化劑
116．．．排放流
118．．．入口壓縮機
120．．．進料氧化劑
122．．．氣態排氣流
124．．．排氣循環系統
126．．．熱回收蒸汽產生器
128．．．蒸汽燃氣渦輪
130．．．蒸汽
132．．．排氣
134．．．冷卻單元
138．．．水漏失流
140．．．經冷卻的循環氣流
141．．．管線
142．．．增壓壓縮機
144．．．經壓縮的循環流
146．．．沖刷流
148．．．CO2分離器
150．．．管線
151．．．殘餘流
152．．．氣體膨脹機
154．．．柄
156．．．排氣

Claims (30)

  1. 一種CO2製造之整合系統(100)，其包含：燃氣渦輪系統(102)，具有配置成在經壓縮的循環流存在下以實質上化學計量地燃燒第一經壓縮的氧化劑與第一燃料之第一燃燒室(110)，使得所供應的氧與化學計量燃燒所需要的氧之比例為0.9：1至1.1：1，其中該燃燒室(110)將第一排放流導向膨脹機(106)，以產生氣態排氣流，且至少部分驅動第一壓縮機(104)；排氣循環系統(124)，其包含至少一個增壓壓縮機，其係配置以在將經冷卻的循環氣體導入該第一壓縮機之前，接收該氣態排氣流並將其增壓，其中該第一壓縮機將該氣態排氣流壓縮，藉以產生該經壓縮的循環流，該經壓縮的循環流作為稀釋劑，係配置以緩和該第一排放流的溫度；CO2分離器(148)，其經由沖刷流與經壓縮的循環流以流體連接；及氣體膨脹機(152)，其經由主要以衍生自該CO2分離器之富氮氣體所組成之殘餘流與該CO2分離器以流體連接。
  2. 如申請專利範圍第1項之系統，其中該排氣循環系統進一步包含至少一個增壓壓縮機(142)，係配置以在將經冷卻的循環氣體導入該第一壓縮機之前接收該氣態排氣流並將其增壓。
  3. 如申請專利範圍第2項之系統，其進一步包含與該至少一個增壓壓縮機以流體連接的第一及第二冷卻單元 (134，136)，該第一冷卻單元係配置以在導入該至少一個增壓壓縮機之前將該氣態排氣流接收及冷卻，且第二冷卻單元係配置以接收該至少一個增壓壓縮機的氣態排氣流，且進一步冷卻該氣態排氣流，以產生該經冷卻的循環氣體。
  4. 如申請專利範圍第1項之系統，其進一步包含加熱器裝置(158)，係用以將該殘餘流加熱，產生熱氮蒸氣流。
  5. 如申請專利範圍第4項之系統，其中該氣體膨脹機係配置以將該熱氮蒸氣膨脹，藉以產生機械動力及排氣。
  6. 如申請專利範圍第5項之系統，其進一步包含由該氣體膨脹機產生的機械動力所驅動的入口壓縮機(118)，其中該入口壓縮機係配置以提供該第一經壓縮的氧化劑。
  7. 如申請專利範圍第4項之系統，其中該加熱器裝置包含與該沖刷流及該殘餘流以流體連接的熱交換器(158)，該熱交換器係配置以降低該沖刷流的溫度，且同時增加該殘餘流的溫度。
  8. 如申請專利範圍第1項之系統，其進一步包含與該沖刷流相關而配置的催化設備(164)，該催化設備係配置以增加該沖刷流在進入該加熱器裝置之前的溫度。
  9. 如申請專利範圍第4項之系統，其中該加熱器裝置包含與該殘餘流以流體連接的第二燃燒室(168)，且該係配置以將第二燃料與第二經壓縮的氧化劑化學計量地燃燒，以產生第二排放流。
  10. 如申請專利範圍第9項之系統，其中該氣體膨脹 機係配置以將該第二排放流膨脹，並藉以產生機械動力及排氣。
  11. 如申請專利範圍第9項之系統，其中該第一與第二經壓縮的氧化劑及該第一與第二燃料係分別衍生自相同來源。
  12. 如申請專利範圍第9項之系統，其中該第二燃料為氫燃料。
  13. 一種產生動力的方法，其包含：在第一燃燒室(110)中及在經壓縮的循環流存在下，將第一經壓縮的氧化劑及第一燃料化學計量地燃燒，使得所供應的氧與化學計量燃燒所需要的氧之比例為0.9：1至1.1：1，藉以產生第一排放流，其中該經壓縮的循環流作為稀釋劑，係配置以緩和該第一排放流的溫度；在膨脹機(106)中將該第一排放流膨脹，以至少部分驅動第一壓縮機(104)，並產生氣態排氣流；將該氣態排氣流導入該第一壓縮機(104)，其中該第一壓縮機將該氣態排氣流壓縮，並藉以產生該經壓縮的循環流；經由沖刷流將一部份之該經壓縮的循環流抽取至CO2分離器(148)，該CO2分離器係經由衍生自該CO2分離器且主要以富氮氣體所組成的殘餘流以流體連接至氣體膨脹機；及在氣體膨脹機(152)中將該殘餘流膨脹，以產生機械動力及排氣。
  14. 如申請專利範圍第13項之方法，其進一步包含增壓壓縮機(142)及冷卻單元(134，136)中之至少一者，係用以增加該氣態排氣流的質量流率，以產生循環氣體。
  15. 如申請專利範圍第14項之方法，其包含以與至少一個增壓壓縮機以流體連接之第一冷卻單元(134)將該氣態排氣流冷卻，該第一冷卻單元係配置以在導入該至少一個增壓壓縮機之前將該氣態排氣流接收及冷卻。
  16. 如申請專利範圍第15項之方法，其進一步包含以與該至少一個增壓壓縮機以流體連接的第二冷卻單元(136)將該至少一個增壓壓縮機的該氣態排氣流冷卻，以產生該循環氣體。
  17. 如申請專利範圍第13項之方法，其進一步包含以氣體膨脹機所產生的機械動力驅動入口壓縮機(118)，該入口壓縮機係配置以產生該第一經壓縮的氧化劑。
  18. 如申請專利範圍第13項之方法，其進一步包含使用加熱器裝置(158)以增加該殘餘流的溫度，以產生熱氮蒸氣流。
  19. 如申請專利範圍第18項之方法，其中該加熱器裝置(158)包含與該沖刷流及該殘餘流二者以流體連接的熱交換器，且進一步包含以熱交換器降低該沖刷流的溫度及增加該殘餘流的溫度，藉以產生熱氮蒸氣流。
  20. 如申請專利範圍第19項之方法，其進一步包含在熱交換器之前，在配置於該沖刷流內之催化設備(164)中，燃燒氧氣及剩餘燃料，以增加該沖刷流的溫度。
  21. 如申請專利範圍第13項之方法，其進一步包含將水注入該熱氮蒸汽流，以增加該氣體膨脹機的質量輸出。
  22. 如申請專利範圍第18項之方法，其中該加熱器裝置包含第二燃燒室(168)，且進一步包含在與該殘餘流以流體連接的該第二燃燒室中，計量化學地燃燒第二燃料及第二經壓縮的氧化劑，該第二燃燒室係配置以產生第二排放流。
  23. 如申請專利範圍第22項之方法，其進一步包含以排放自CO2分離器的該殘餘流來緩和該第二排放流的溫度。
  24. 如申請專利範圍第20項之方法，其進一步包含在該氣體膨脹機中將該第二排放流膨脹，以產生機械動力以驅動入口壓縮機(118)，該入口壓縮機係配置以產生該第一經壓縮的氧化劑。
  25. 一種CO2製造之整合系統，其包含第一燃氣渦輪系統(102)，其包含：第一壓縮機(104)，係配置以接收及壓縮循環排氣，及提供第一經壓縮的循環流；第一燃燒室(110)，係配置以接收該第一經壓縮的循環流、第一經壓縮的氧化劑、及第一燃料流，該第一燃燒室係用以將該第一燃料流及該第一經壓縮的氧化劑實質上化學計量地燃燒，使得所供應的氧與化學計量燃燒所需要的氧之比例為0.9：1至1.1：1，其中該第一經壓縮的循環流作為稀釋劑， 以緩和燃燒溫度；及與該第一壓縮機連接的第一膨脹機(106)，且配置以接收該第一燃燒室的第一排放物，且產生循環排氣及至少部分驅動該第一壓縮機；CO2分離器(142)，其係配置以接收和處理取自該經壓縮的循環流之沖刷流，以提供CO2流及殘餘流，該殘餘流實質上包含氮氣；及第二燃氣渦輪系統(702)，其係經由該沖刷流與該第一燃氣渦輪系統以流體連接，該第二燃氣渦輪系統(702)包含：第二壓縮機(176)，係配置以將進料氧化劑接收及壓縮，及產生第二經壓縮的氧化劑，該第一經壓縮的氧化劑係至少部分衍生自該第二經壓縮的氧化劑；第二燃燒室(168)，係配置以接收該第二經壓縮的氧化劑、來自該殘餘流的氮氣、及該第二燃料流，該第二燃燒室係用以將該第二燃料流及該第二經壓縮的氧化劑化學計量地燃燒，其中該氮氣作為稀釋劑，以緩和燃燒溫度；及與該第二壓縮機連接的第二膨脹機(178)，且配置以接收該第二燃燒室的第二排放物，並產生排氣及至少部分驅動該第二壓縮機。
  26. 如申請專利範圍第25項之系統，其中該第一燃氣渦輪系統進一步包含增壓壓縮機(142)，係配置以在注入該 第一壓縮機之前增加該循環排氣的壓力，以提供該經壓縮的循環流。
  27. 如申請專利範圍第26項之系統，其中該第二燃料為氫燃料。
  28. 如申請專利範圍第26項之系統，其中該第二燃氣渦輪系統進一步包含熱回收蒸汽產生器(126)，係配置以接收該第二膨脹機的排氣，並對蒸汽燃氣渦輪提供蒸汽。
  29. 一種CO2製造之整合系統，其包含：燃氣渦輪系統(102)，具有配置成在經壓縮的循環流存在下以化學計量地燃燒經壓縮的氧化劑與燃料之第一燃燒室(110)，使得所供應的氧與化學計量燃燒所需要的氧之比例為0.9：1至1.1：1，其中該燃燒室(110)對膨脹機(106)提供排放流，以產生氣態排氣流，且至少部分驅動第一壓縮機(104)；排氣循環系統(124)，其具有至少一個增壓壓縮機(142)，其係配置以在將經冷卻的循環氣體導入該第一壓縮機(104)之前接收該氣態排氣流並增加其壓力，其中該第一壓縮機(104)將該經冷卻的循環氣體壓縮，並藉以產生該經壓縮的循環流，該經壓縮的循環流作為稀釋劑，係配置以緩和該排放流的溫度；CO2分離器(148)，其經由沖刷流與該經壓縮的循環流以流體連接；及下游壓縮機(188)，其經由以衍生自該CO2分離器且主要由富氮氣體所組成之殘餘流與該CO2分離器以流體連 接。
  30. 如申請專利範圍第29項之系統，其中該下游壓縮機(188)係配置以將該富氮氣體壓縮以維持壓力。
TW100120161A 2010-07-02 2011-06-09 低排放之三循環動力產生系統和方法 TWI564475B (zh)

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AR081784A1 (es) 2012-10-17
EP2588729B1 (en) 2020-07-15
EA201390054A1 (ru) 2013-04-30
CA2801488A1 (en) 2012-01-05
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US20130104563A1 (en) 2013-05-02
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TW201219644A (en) 2012-05-16
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WO2012003077A1 (en) 2012-01-05
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