TW201303144A - 低排放組合式渦輪機系統中用於攫取二氧化碳之系統與方法 - Google Patents

低排放組合式渦輪機系統中用於攫取二氧化碳之系統與方法 Download PDF

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TW201303144A
TW201303144A TW101106769A TW101106769A TW201303144A TW 201303144 A TW201303144 A TW 201303144A TW 101106769 A TW101106769 A TW 101106769A TW 101106769 A TW101106769 A TW 101106769A TW 201303144 A TW201303144 A TW 201303144A
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Franklin F Mittricker
Omar Angus Sites
Sulabh K Dhanuka
Richard Huntington
Dennis O'dea
Russell H Oelfke
Robert Dean Denton
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Exxonmobil Upstream Res Co
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Abstract

本發明提供於組合式低排放渦輪機系統中產生動力及從排氣攫取及回收二氧化碳之系統、方法與設備。在一或多個具體例中，將來自多個渦輪機系統之排氣組合、冷卻、壓縮及分離，得到含二氧化碳之流出物流及含氮之產物流。經再循環之排氣流及產物流的部分可作為稀釋劑，以調節在渦輪機系統的各燃燒器中之燃燒。

Description

低排放組合式渦輪機系統中用於攫取二氧化碳之系統與方法
本申請案主張在2011年9月30日以低排放組合式渦輪機系統中用於攫取二氧化碳的系統與方法(SYSTEMS AND METHODS FOR CARBON DIOXIDE CAPTURE IN LOW EMISSION COMBINED TURBINE SYSTEMS)為標題提出申請之美國臨時專利申請案第61/542,039號；在2011年3月22日以具有主空氣壓縮機氧化劑控制設備的低排放渦輪機系統以及其相關方法(LOW EMISSION TURBINE SYSTEMS HAVING A MAIN AIR COMPRESSOR OXIDANT CONTROL APPARATUS AND METHODS RELATED THERETO)為標題提出申請之美國臨時專利申請案第61/466,384號；在2011年9月30日以併有進氣口壓縮機氧化劑控制設備的低排放渦輪機系統以及其相關方法(LOW EMISSION TURBINE SYSTEMS INCORPORATING INLET COMPRESSOR OXIDANT CONTROL APPARATUS AND METHODS RELATED THERETO)為標題提出申請之美國臨時專利申請案第61/542,030號；在2011年3月22日以固定式幾何學氣渦輪機系統之化學計量燃燒的控制方法以及其相關設備與系統(METHODS FOR CONTROLLING STOICHIOMETRIC COMBUSTION ON A FIXED GEOMETRY GAS TURBINE SYSTEM AND APPARATUS AND SYSTEMS RELATED THERETO)為標題提出申請之美國臨時專利申請案第61/466,385號；在2011年9月30日以低排放渦輪機系統 中之化學計量燃燒的控制系統與方法(SYSTEMS AND METHODS FOR CONTROLLING STOICHIOMETRIC COMBUSTION IN LOW EMISSION TURBINE SYSTEMS)為標題提出申請之美國臨時專利申請案第61/542,031號；在2011年3月22日以低排放渦輪氣體循環迴路的變動方法以及其相關系統與設備(METHODS OF VARYING LOW EMISSION TURBINE GAS RECYCLE CIRCUITS AND SYSTEMS AND APPARATUS RELATED THERETO)為標題提出申請之美國臨時專利申請案第61/466,381號；在2011年9月30日以低排放渦輪氣體循環迴路的變動方法以及其相關系統與設備(METHODS OF VARYING LOW EMISSION TURBINE GAS RECYCLE CIRCUITS AND SYSTEMS AND APPARATUS RELATED THERETO)為標題提出申請之美國臨時專利申請案第61/542,035號之優先權，將該等以其全文特此併入以供參考。
本申請案與下列者有關：在2011年9月30日以低排放渦輪機系統中用於攫取二氧化碳的系統與方法(SYSTEMS AND METHODS FOR CARBON DIOXIDE CAPTURE IN LOW EMISSION TURBINE SYSTEMS)為標題提出申請之美國臨時專利申請案第61/542,036號；在2011年9月30日以低排放渦輪機系統中用於攫取二氧化碳的系統與方法(SYSTEMS AND METHODS FOR CARBON DIOXIDE CAPTURE IN LOW EMISSION TURBINE SYSTEMS)為標題提出申請之美國臨時專利申 請案第61/542,037號；在2011年9月30日以併有二氧化碳分離的低排放動力產生系統及方法(LOW EMISSION POWER GENERATION SYSTEMS AND METHODS INCORPORATING CARBON DIOXIDE SEPARATION)為標題提出申請之美國臨時專利申請案第61/542,041號；將所有該等以其全文特此併入以供參考。
本揭露的具體例係關於低排放動力產生。更特定言之，本揭露的具體例係關於低排放組合式氣渦輪機系統中用於攫取二氧化碳以增加效率及降低成本之方法與設備。
此段落意欲介紹本技藝的各種態樣，其可與本揭露的示範性具體例相關聯。咸信此討論有助於提供促進更瞭解本揭露的特殊態樣之架構。據此，應瞭解應以此見解閱讀此段落，而未必為承認的先前技藝。
許多產油國家正遭遇國內動力需求的強力成長，且對提高石油料回收(EOR)有興趣，以改進其貯油槽的油料回收。二種常見的EOR技術包括用於貯油槽壓力維持的氮(N2)注入法及用於EOR之混溶驅油的二氧化碳(CO2)注入法。亦有關於溫室氣體(GHG)排放的全球議題。在許多國家中與總量管制與交易(cap-and-trade)政策之實施結合的此議題使那些國家以及於國家中操作烴製造系 統的公司以降低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溶劑(諸如胺類)的後燃燒攫取。然而，此二種解決方法昂貴且降低動力產生效率，導致較低的動力產量、增加燃料需求及增加電力成本，以符合國內的動力需求。特別是氧、SOx及NOx成分的存在使得胺溶劑吸收的利用大有問題。另一方法為組合式循環中的含氧燃料氣渦輪機(例如，在此攫取來自氣渦輪機布雷頓(Brayton)循環的排氣熱，以製造蒸汽且在蘭金(Rankin)循環中生產額外的動力)。然而，沒有任何可於此一循環中操作的市售氣渦輪機且生產高純度氧所需之動力顯著地降低此方法的總效率。
而且，隨著關於全球氣候變化的議題高漲及二氧化碳排放的衝擊，已將重點放在使動力廠的二氧化碳排放減至最低。氣渦輪動力廠具有效率且與核或煤動力產生技術相比而具有較低的成本。然而，自氣渦輪動力廠的排氣攫取二氧化碳非常昂貴，因為在排氣煙囪中的二氧化碳濃度低，需要處理大體積的氣體，及排氣流的壓力低。所有該等因素尤其導致高成本的二氧化碳攫取。
據此，對在降低成本下併有CO2攫取及回收之低排放、高效率動力產生方法仍有很大的需求。
在本文所述之低排放動力產生系統中，反而將來自低排放氣渦輪機之排氣(其係在典型的天然氣組合式循環( NGCC)廠中排出)分離且回收。將本發明的設備、系統與方法組合且再循環兩個氣渦輪機的排氣流，以有效地產生動力，同時濃縮及回收二氧化碳。
在本發明的系統與方法中，將各包含壓縮機、燃燒室及膨脹器的兩個氣渦輪系統經流體連結以串接操作且將各系統的排氣組合。接著將組合的排氣冷卻、壓縮且再循環。將經再循環之排氣流的一部分供給至燃燒室之一中用作為稀釋劑，以控制或以另外方式緩和燃燒溫度及進入後繼膨脹器的煙道氣溫度。將經再循環之排氣流的另一部分分離，以攫取在一個流中的CO2且產生包含氮、氧、氬或其組合之分開的產物流。接著將來自CO2分離器之產物流的一部分同樣地供給至其他的燃燒室中用作為稀釋劑，而產物流的餘留部分可用於產生額外的動力或用於系統內或外部的另一目的。藉由此方式組合排氣而使來自整體系統內的各氣渦輪機之燃燒產物濃縮且可更容易攫取及移除CO2，從而造成更有效的動力產生。
在以下的詳細說明段落中，本揭露的特定具體例係連同較佳的具體例予以說明。然而，以下說明在一定程度上係專對於本揭露的特殊具體例或特殊用途，其意欲以示範為目的而已，且簡單地提供示範性具體例的說明。據此，本揭露並不受限於下文所述之特定具體例，但反而包括所有落在隨附之申請專利範圍的真正精神及範圍內之替代方 案、修改及同等物。
如本文所使用之各種術語係定義於下。在申請專利範圍內所使用之術語在一定程度上未定義於下，應給予由相關技藝者按照至少一種經印刷之出版品或頒予之專利中所反映的術語給予之最廣定義。
如本文所使用之術語〝天然氣〞係指從原油井(聯產氣)及/或從含氣體之地下岩層(非聯產氣)所獲得的多成分氣體。天然氣的組成及壓力可顯著變動。典型的天然氣流含有甲烷(CH4)為主要成分，亦即大於天然氣流的50莫耳%為甲烷。天然氣流亦可含有乙烷(C2H6)、較高分子量的烴(例如，C3-C20烴)、一或多種酸氣體(例如，硫化氫)或其任何組合。天然氣亦可含有少量污染物，諸如水、氮、硫化鐵、蠟、原油或其任何組合。
如本文所使用之術語〝化學計量燃燒〞係指具有包含燃料及氧化劑的反應物體積及藉由燃燒反應物所形成之產物體積的燃燒反應，其中整個反應物體積皆用於形成產物。如本文所使用之術語〝實質的化學計量燃燒〞係指具有從約0.9：1至約1.1：1，或更佳從約0.95：1至約1.05：1為範圍之當量比的燃燒反應。本文所使用之術語〝化學計量〞意謂包含化學計量及實質的化學計量條件兩者，除非另有其他指示。
如本文所使用之術語〝流〞係指流體的體積，雖然術語流的使用典型地意謂流體的移動體積(例如，具有速度或質量流率)。然而，術語〝流〞不需要速度、質量流率 或圍住流的特殊管道類型。
目前所揭示之系統與方法的具體例可用於生產低排放電力及用於提高油料回收(EOR)或隔離應用的CO2。根據本文所揭示之具體例，可將經壓縮之氧化劑(典型為空氣)與燃料的混合物在兩個分開但經流體連結的氣渦輪機的燃燒室中燃燒且將來自各室之排氣膨脹，以產生動力。接著將排氣組合、冷卻、壓縮及分離，以攫取CO2及產生包含氮之產物流。在EOR應用中，將回收之CO2注入產油井或與產油井毗鄰，經常係在超臨界條件下。CO2同時用作為加壓劑及在溶解於地下原油中時顯著地降低油的黏度，能使油更快流經地面至移出井。包含氮之產物流(且亦時常包含氧和氬)可用於產生額外的動力，且亦可用於各種目的，包括壓力維持應用。在壓力維持應用中，將惰性氣體(諸如氮)壓縮且注入烴貯存器中，以維持貯存器中的原始壓力，因此容許提高烴回收。本文所揭示之系統的結果係以更具經濟效益的方式下生產動力及濃縮且攫取CO2。
在本發明的一或多個具體例中提供動力產生系統，其包含第一壓縮機，其係經配置以接收且壓縮一或多種氧化劑，以產生經壓縮之氧化劑；第一燃燒室，其係經配置以接收且燃燒經壓縮之氧化劑的第一部分、至少一種第一燃料及第一稀釋劑，以產生第一排氣流；及第一膨脹器，其係經配置以接收第一排氣流且產生第一氣態排氣流。該系統另外包含第二壓縮機，其係經配置以接收且壓縮經冷卻 之再循環流，以產生經壓縮之再循環流；第二燃燒室，其係經配置以接收且燃燒經壓縮之氧化劑的第二部分、至少一種第二燃料及第二稀釋劑，以產生第二排氣流；及第二膨脹器，其係經配置以接收第二排氣流且產生第二氣態排氣流。該系統另外包含一或多個熱回收蒸汽產生器，其係經配置以接收且冷卻第一及第二氣態排氣流，以產生蒸汽及經組合之排氣流；再循環冷卻單元，其係經配置以接收且冷卻經組合之排氣流，並產生經冷卻之再循環流；及分離器，其係經配置以接收且分離經壓縮之再循環流的一部分成為分離器流出物流及分離器產物流。
一或多種氧化劑可包含任何含氧流體，諸如周圍空氣、富氧空氣、實質的純氧或其組合。在一或多個本發明之具體例中，將供給至組合式系統中的全部或實質上全部的氧化劑完全在第一壓縮機中壓縮及由第一壓縮機供給。接著可將排離第一壓縮機的經壓縮之氧化劑分裂成兩個流，得以將經壓縮之氧化劑的第一部分引導至第一燃燒室及將經壓縮之氧化劑的第二部分引導至第二燃燒室。分裂流可相等或不相等，且亦可在操作期間變動以適應製程變化。
第一及第二燃料可相同或不同，且各燃料可包含天然氣、聯產氣、柴油、燃料油、氣化煤、煤焦、石腦油、丁烷、丙烷、合成氣、煤油、航空燃料、生質燃料、加氧之烴原料、任何其他適合的含烴氣體或液體、氫或其組合。另外，燃料可包含惰性成分，包括但不限於N2或CO2。在一些具體例中，第一燃料及/或第二燃料可至少部分由 烴貯存器供給，此烴貯存器係經由注入由本文所述之方法所攫取之CO2而受惠於提高之油料回收。在特定的具體例中，第一及第二燃料包含天然氣。
在第一及第二燃燒室之各者中的燃燒條件可為貧條件、化學計量或實質的化學計量條件或富條件。在一或多個具體例中，在第一及第二燃燒室中的燃燒條件為化學計量或實質的化學計量。將第一及第二稀釋劑供給至第一及第二燃燒室，以控制或以另外方式調節燃燒及煙道氣溫度，以符合後繼膨脹器的材料要求。然而，亦可調整第一及第二稀釋劑的流量以助於維持在各自燃燒室中的化學計量條件、緩和組成物變化、體積流量或在氧化劑及燃料流中的其他變化。在一或多個具體例中，提供至第一燃燒室之第一稀釋劑包含分離器產物流的至少一部分。在相同或其他的具體例中，提供至第二燃燒室之第二稀釋劑包含經壓縮之再循環流的至少一部分。
在一些具體例中，高壓蒸汽亦可用作為第一及第二燃燒室之一或兩者中的冷卻劑。在此等具體例中，添加蒸汽可減少系統中的動力及尺寸要求，但可能需要加入水再循環迴路或迴路等。另外，在更多具體例中，到達燃燒室之一或兩者的經壓縮之氧化劑進料可包含氬。例如，氧化劑可包含從約0.1至約5.0體積%之氬，或從約1.0至約4.5體積%之氬，或從約2.0至約4.0體積%之氬，或從約2.5至約3.5體積%之氬，或約3.0體積%之氬。
第一及第二壓縮機可各自為單一壓縮機或可為二或多 個並聯或串聯操作的壓縮機。各壓縮機可包含單階段或多階段。在多階段壓縮機中，可隨意地使用階段間冷卻而容許較高的總壓縮比及較高的總動力輸出。當使用一個以上的壓縮機壓縮製程流時，則連在一起的壓縮機在本文於適當時被視為〝第一壓縮機〞或〝第二壓縮機。各壓縮機可具有任何適合於本文所述之方法的類型。此等壓縮機包括但不限於軸式、離心式、往復式或雙螺旋式壓縮機及其組合。在一或多個具體例中，第一及第二壓縮機為軸式壓縮機。
氧化劑與燃料在第一及第二燃燒室之各者中的燃燒分別產生第一排氣流及第二排氣流。第一及第二排氣流包含燃燒產物，且該等個別的組成將取決於各燃燒室中所使用之燃料及氧化劑的組成而變動。在一或多個具體例中，第一及第二排氣流可各自包含蒸發之水、CO2、一氧化碳(CO)、氧(O2)、氮(N2)、氬(Ar)、氮氧化物(NOX)、硫氧化物(SOX)、硫化氫(H2S)或其組合。
第一排氣流可在第一膨脹器中膨脹，以形成第一氣態排氣流，而第二排氣流可在第二膨脹器中膨脹，以形成第二氣態排氣流。第一及第二膨脹器可各自為單一膨脹器或可為二或多個並聯或串聯操作的膨脹器。各膨脹器可包含單階段或多階段。當使用超過一個的膨脹器膨脹排氣流時，則連在一起的膨脹器在本文於適當時被視為〝第一膨脹器〞或〝第二膨脹器〞。各膨脹器可為任何適合於本文所述之方法的膨脹器類型，包括但不限於軸式或離心式膨脹 器或其組合。第一及第二排氣流的膨脹產生動力，其可用於驅動一或多個壓縮機或發電機。在本發明的一或多個具體例中，第一膨脹器係經由共軸或其他機械、電或其他動力耦接而與第一壓縮機耦接，使得第一壓縮機至少部分由第一膨脹器驅動。在相同或其他的具體例中，第二膨脹器係經由共軸或其他機械、電或其他動力耦接而與第二壓縮機耦接，使得第二壓縮機至少部分由第二膨脹器驅動。在其他的具體例中，第一或第二壓縮機或兩者可與具有或不具有增速或減速裝置(諸如齒輪箱)的電動馬達經機械耦接。當連在一起時，則第一壓縮機、第一燃燒室及第一膨脹器可以布雷頓循環為特徵。第二壓縮機、第二燃燒室及第二膨脹器亦同樣可以布雷頓循環為特徵。
在膨脹之後，第一及第二氣態排氣流在一些具體例中可於熱回收蒸汽產生器(HRSG)中冷卻。雖然在本文述及單一HRSG，但實際上可使用二或多個HRSG。另一選擇地，可使用任何經設計以冷卻或回收第一及第二氣態排氣流的熱之裝置代替HRSG，諸如一或多個熱交換器、再生器、冷卻單元或類似物。HRSG可經配置以接收第一及第二排氣流且利用流中的殘餘熱產生蒸汽。由HRSG所產生之蒸汽可用於各種目的，諸如驅動在蘭金循環中的蒸汽渦輪產生器或用於水脫鹽作用。
在本發明的一或多個具體例中，將第一及第二氣態排氣流分開進料至HRSG且在HRSG內組合，以形成經組合之排氣流。在其他的具體例中，第一及第二氣態排氣流可 在HRSG的上游或下游組合。當流在下游組合時，可將第一及第二氣態排氣流之各者在分開的HRSG中冷卻且接著組合，以形成經組合之排氣流。
在本發明的一或多個具體例中，可將經組合之排氣流送至一或多個冷卻單元，其係經配置以降低經組合之排氣流的溫度且產生經冷卻之再循環流。冷卻單元可為任何適合於降低排氣溫度的設備類型，諸如直接接觸冷卻器(DCC)、蛇行管冷卻器、機械冷凍單元或其組合。在一些具體例中，冷卻單元為DCC。冷卻單元亦可經配置以經由水漏失流移除經冷卻之再循環流的經冷凝之水的一部分。在一些具體例中，水漏失流可隨意地按路徑至HRSG，以提供產生額外蒸汽之水源。
在一些具體例中，可將排離冷卻單元的經冷卻之再循環流送至第二壓縮機且壓縮，以產生經壓縮之再循環流。冷卻且壓縮排氣有助於對付與一般造成高成本的CO2攫取之必須處理的大體積氣體及低壓排氣流有關之爭議，因此使本發明系統中的CO2攫取及回收更有效率且更具成本效益。
在排離第二壓縮機時，可將經壓縮之再循環流分裂，且可將經壓縮之再循環流的第一部分提供至第二燃燒室用作為稀釋劑，如先前所述。在此等事例中，可將不引導至第二燃燒室的經壓縮之再循環流的第二部分進料至一或多個分離器中，其中將CO2及其他溫室氣體與經壓縮之再循環流分離。雖然未於本文詳細說明，但是那些熟諳本技藝 者應察知在第二壓縮機與分離器之間可能需要中間加熱、冷卻或其他製程操作，所以再循環流係在使所使用之特別的分離法最優化之條件下進入分離器中。例如，在一或多個具體例中，冷卻單元可用於冷卻在進入分離器之前的經壓縮之再循環流。
在一或多個分離器中所使用之CO2分離法可為任何經設計以分離經壓縮之再循環氣體且生成包含CO2之分離器流出物流及包含氮之分離器產物流的適合方法。在一些具體例中，產物流亦可包含氧、氬或兩者。分離經壓縮之再循環流的成分容許排氣中的不同成分以不同的方式處置。分離法可理想地隔離在排氣中的所有溫室氣體(諸如CO2、CO、NOx、SOx等)於流出物流中，排氣成分的餘留部分(諸如氮、氧和氬)係留在產物流中。然而，實際上分離法不可能自產物流抽出所有的溫室氣體，而一些非溫室氣體可餘留在流出物流中。
可使用任何經設計以達成所欲結果之適合的分離法。在一或多個具體例中，分離法為氧遲鈍法。適合的分離法之實例包括但不限於熱碳酸鉀(〝熱鍋〞)分離法、胺分離法、分子篩分離法、薄膜分離法、吸附動力學分離法、受控制之冷凍區分離法及其組合。在一些具體例中，分離器係使用熱鍋分離法。在本發明的一或多個具體例中，分離法可在升壓下操作(亦即比周圍壓力高)且經配置以保持加壓之產物流。以此方式維持分離法之壓力容許較小的分離裝備，提供改進之分離有效性及容許增加自產物流的 能量提取。在一些具體例中，CO2分離法的選擇及配置使產物流之出氣口壓力或出氣口溫度或兩者達到最大。
分離器流出物流可用於各種應用。例如，可將流出物流注入烴貯存器中以供提高油料回收(EOR)或可引導至貯存器中以供碳隔離或貯存。亦可將分離器流出物流銷售、排出或閃燄(flared)。
在一或多個具體例中，分離器產物流包含氮及亦隨意地包含氧或氬(或兩者)。可將分離器產物流分裂，且可將產物流的第一部分提供至第一燃燒室用作為稀釋劑，如先前所述。在此等事例中，可將未引導至第一燃燒室的分離器產物流的第二部分引導至第三膨脹器。在一或多個具體例中，第三膨脹器可經配置以接收分離器產物流且在約周圍壓力下輸出相同的氣體。如那些熟諳本技藝者所察知，第三膨脹器產生動力，且所產生之動力可用於驅動在所述系統內或外部的一或多個任何構造之壓縮機或發電機。
在一或多個具體例中，產物流可在膨脹後通過一或多個額外的熱回收蒸汽產生器(HRSG)。一或多個HRSG可經配置以利用在流中的殘餘熱以產生蒸汽。由一或多個HRSG所產生之蒸汽可用於各種目的，諸如驅動在蘭金循環中的蒸汽渦輪產生器或用於水脫鹽作用。再者，若任何殘餘熱餘留在排離一或多個HRSG之產物流中，則系統可另外包含一或多個經配置以轉移熱至無蒸汽運轉流體的熱交換器。在此等具體例中，無蒸汽運轉流體可隨意地用於驅動蘭金循環中的膨脹器。
分離器產物流可全部或部分用於各種應用。例如，可將產物流注入烴貯存器中以供壓力維持。亦可將產物流銷售或排出。在一或多個具體例中，當壓力維持是不可行的選擇時(或當僅需要產物流的一部分用於壓力維持時)，可將產物流以膨脹或另一方法冷卻，且用於提供本文所述之系統中的冷凍。例如，經冷卻之產物流可用於提供冷凍，以降低在系統內的一或多個壓縮機的抽氣溫度，或驟冷用於系統內的一或多個冷卻單元中之水。
在其他的具體例中，當產物流的全部或一部分不用於壓力維持時，反而可將產物流加熱，所以可產生額外的動力供系統中的別處使用或供銷售。加熱產物流的一些方法包括將產物流與另一製程流在熱交換器中交叉交換，或使用補充的燃燒器供給額外的熱至產物流。應察知使用額外的燃燒器需要額外的燃料。若在燃燒器中使用含碳燃料，則產生不可自產物流回收之額外的CO2。因此，在一些具體例中，在燃燒器中所使用的燃料可為非碳燃料來源，諸如氫。補充的燃燒器所需之氧化劑可經由分開的氧化劑流供給，或可在產物流中有足夠的氧化劑，所以不必額外供給氧化劑。用於加熱分離器產物流的其他可能方法包括在HRSG中使用加熱迴管加熱產物流，使用催化燃燒在產物流中存在的任何CO，或使用產物流冷卻的結果而使流加熱(亦即當產物流提供其他流或設備冷卻時，使流本身被加熱)。
現參考圖形，圖1例證組合式動力產生系統100，其 係經配置以提供在燃燒後分離及攫取CO2。在至少一個具體例中，動力產生系統100可具有經由共軸108或其他機械、電或其他動力耦接而與第一膨脹器106耦接之第一壓縮機118，從而容許由第一膨脹器106所產生之機械能的一部分驅動第一壓縮機118。第一膨脹器106亦可產生供其他用途的動力，諸如發動另一壓縮機、發電機或類似物。第一壓縮機118及第一膨脹器106可分別構成標準的氣渦輪機之壓縮機及膨脹器的末端。然而，在其他的具體例中，第一壓縮機118及第一膨脹器106可為系統中的個別化組件。
系統100亦可包括第一燃燒室110，其經配置以燃燒與經壓縮之氧化劑114的第一部分混合的第一燃料流112。在一或多個具體例中，第一燃料流112可包括任何適合的烴氣體或液體，諸如天然氣、甲烷、石腦油、丁烷、丙烷、合成氣、柴油、煤油、航空燃料、煤衍生之燃料、生質燃料、加氧之烴原料或其組合。第一燃料流112亦可包含氫。供給至第一燃燒室110的經壓縮之氧化劑114的第一部分可得自與第一燃燒室110經流體耦接且適合於壓縮氧化劑進料120之第一壓縮機118。雖然本文的討論係假定氧化劑進料120為周圍空氣，但是氧化劑可包含任何適合的含氧氣體，諸如空氣、富氧空氣、實質的純氧或其組合。在一或多個具體例中，連在一起的第一壓縮機118、第一燃燒室110及第一膨脹器106可以布雷頓循環為特徵。
第一排氣流116係由第一燃料流112與經壓縮之氧化劑114的第一部分之燃燒產物而產生且引導至第一膨脹器106的進氣口。在至少一個具體例中，第一燃料流112主要可為天然氣，從而產生包括蒸發之水、CO2、CO、氧、氮、氬、氮氧化物(NOx)及硫氧化物(SOx)之體積部分的第一排氣流116。在一些具體例中，未燃燒之第一燃料112的一小部分或其他化合物亦可由於燃燒平衡的限制而存在於第一排氣流116中。當第一排氣流116經過第一膨脹器106膨脹時，其產生機械動力以驅動第一壓縮機118或其他設施，且亦生產第一氣態排氣流122。
動力產生系統100亦可具有經由共軸188或其他機械、電或其他動力耦接而與第二膨脹器170耦接之第二壓縮機180，從而容許由第二膨脹器170所產生之機械能的一部分驅動第二壓縮機180。第二膨脹器170亦可產生供其他用途的動力，諸如發動另一壓縮機、發電機或類似物。第二壓縮機180及第二膨脹器170可分別構成標準的氣渦輪機之壓縮機及膨脹器的末端。然而，在其他的具體例中，第二壓縮機180及第二膨脹器170可為系統中的個別化組件。
系統100亦可包括第二燃燒室150，其經配置以燃燒與經壓縮之氧化劑114的第二部分混合的第二燃料流152。在一或多個具體例中，第二燃料流152可包括任何適合的烴氣體或液體，諸如天然氣、甲烷、石腦油、丁烷、丙烷、合成氣、柴油、煤油、航空燃料、煤衍生之燃料、生 質燃料、加氧之烴原料或其組合。第二燃料流152亦可包含氫。供給至第二燃燒室150的經壓縮之氧化劑114的第二部分可得自與第二燃燒室150經流體耦接之第一壓縮機118。在一或多個具體例中，連在一起的第二壓縮機180、第二燃燒室150及第二膨脹器170可以布雷頓循環為特徵。
第二排氣流156係由第二燃料流152與經壓縮之氧化劑114的第二部分之燃燒產物而產生且引導至第二膨脹器170的進氣口。在至少一個具體例中，第二燃料流152主要可為天然氣，從而產生包括蒸發之水、CO2、CO、氧、氮、氬、氮氧化物(NOx)及硫氧化物(SOx)之體積部分的第二排氣流156。在一些具體例中，未燃燒之第二燃料152的一小部分或其他化合物亦可由於燃燒平衡的限制而存在於第二排氣流156中。當第二排氣流156經過第二膨脹器170膨脹時，其產生機械動力以驅動第二壓縮機180或其他設施，且亦生產第二氣態排氣流172。
將分別來自第一膨脹器106及第二膨脹器170的第一及第二氣態排氣流122及172引導至熱回收蒸汽產生器(HRSG)126，其係經配置以使用在氣態排氣流122及172中的殘餘熱，以產生蒸汽130及經組合之排氣流132。由HRSG 126所產生的蒸汽130可具有各種用途，諸如藉由驅動在蘭金循環中的蒸汽渦輪產生器而產生額外的動力或用於水脫鹽作用。
可將經組合之排氣132送至至少一個冷卻單元134， 其係經配置以降低經組合之排氣132的溫度且產生經冷卻之再循環流140。在一或多個具體例中，冷卻單元134在本文考慮為直接接觸冷卻器(DCC)，但是可為任何適合的冷卻裝置，諸如直接接觸冷卻器、蛇行管冷卻器、機械冷凍單元或其組合。冷卻單元134亦可經配置以經由水漏失流136移除經冷凝之水的一部分。
在一或多個具體例中，可將經冷卻之再循環流140引導至與冷卻單元134經流體耦接之第二壓縮機180。第二壓縮機180可經配置以增加經冷卻之再循環流140的壓力，從而產生經壓縮之再循環流182。在排離第二壓縮機180時，可將經壓縮之再循環流182分裂，使得經壓縮之再循環流182的一部分引導至第二燃燒室150，其在該室中用作為稀釋劑，以調節在第二燃燒室150內的燃燒條件。
在一或多個具體例中，將未引導至第二燃燒室的經壓縮之再循環流182的餘留部分引導至分離器162。分離器162可使用各種分離法中之任一者，該分離法係經設計將經壓縮之再循環流182分離成包含CO2之分離器流出物流166及通常包含氮與在一些事例中的氧及/或氬之分離器產物流164。例如，分離器162可經設計將經壓縮之再循環流182使用化學分離法分離，諸如熱碳酸鉀(〝熱鍋〞)分離法、胺分離法或使用分子篩之分離法。其他的分離法包括使用薄膜之物理分離法，或諸如吸附動力學分離法或受控制之冷凍區分離法之方法。在一些具體例中，可使用 前述分離法之組合。在一或多個具體例中，CO2分離法可經配置而使產物流164的溫度或壓力達到最大。分離器流出物流166可用於各種下游應用，諸如注入烴貯存槽中以供提高油料回收(EOR)、碳隔離、貯存或銷售。亦可將流出物流166排出或閃燄。
在一或多個具體例中，可將排離分離器162之產物流164的一部分轉移且以再循環之產物流184引導至第一燃燒室110。在此方式中，再循環之產物流184可用作為稀釋劑，以調節在第一燃燒室110內的燃燒條件。接著可將產物流164的餘留部分用於產生額外的動力。例如，可將產物流164引導至第三膨脹器190。由第三膨脹器190所產生之動力可用於各種目的，諸如至少部分驅動一或多個額外的壓縮機(未顯示)或驅動發電機。在一些具體例中，當產物流注入貯存器中以供壓力維持時，第三膨脹器190可用於驅動管道或噴射壓縮機。
在一或多個具體例中，可將排離第三膨脹器190的經膨脹之產物流192引導至熱回收蒸汽產生器(未顯示)，以產生額外的動力。與流出物流166一樣，產物流192亦可用於各種其他應用，包括壓力維持、貯存或排出。
現參考圖2，其描述圖1之動力產生系統100的替代構造，以系統200具體化及說明。如此，可參考圖1而對圖2有最好的瞭解。在圖2之系統200中，將第一氣態排氣流122與第二氣態排氣流172在HRSG 126的上游組合，以形成經組合之排氣流132。接著將經組合之排氣流 132引導至HRSG 126，以冷卻經組合之排氣流132及產生蒸汽130，而系統的其餘部分係如關於圖1之先前所述方式操作。
現參考圖3，其描述圖1之動力產生系統100的替代構造，以系統300具體化及說明。在圖3之系統300中，將氣態排氣流之各者在組合之前分開冷卻。尤其將第一氣態排氣流122在HRSG 126中冷卻，而將第二氣態排氣流172在另一HRSG 326中冷卻。第一及第二氣態排氣流122及172分別排離HRSG 126及326，且接著在HRSG的下游組合，以形成經組合之排氣流132。系統的其餘部分係如關於圖1之先前所述方式操作。
雖然本揭露可容許各種修改及替代形式，但是上文所討論的示範性具體例僅以實例的方式顯示。本文所述之任何具體例的任何特性或構造可與任何其他具體例或與多樣的其他具體例(至可實行的程度)組合，且意欲使所有此等組合在本發明的範圍內。另外，應瞭解不意欲使本揭露受限於本文所揭示的特殊具體例。事實上，本揭露包括所有落在隨附之申請專利範圍的真正精神及範圍內之替代方案、修改及同等物。
100,200,300‧‧‧動力產生系統
106‧‧‧第一膨脹器
108,188‧‧‧共軸
110‧‧‧第一燃燒室
112‧‧‧第一燃料流
114‧‧‧經壓縮之氧化劑
116‧‧‧第一排氣流
118‧‧‧第一壓縮機
120‧‧‧氧化劑進料
122‧‧‧第一氣態排氣流
126,326‧‧‧熱回收蒸汽產生器(HRSG)
130‧‧‧蒸汽
132‧‧‧經組合之排氣流
134‧‧‧冷卻單元
136‧‧‧水漏失流
140‧‧‧經冷卻之再循環流
150‧‧‧第二燃燒室
152‧‧‧第二燃料流
156‧‧‧第二排氣流
162‧‧‧分離器
164‧‧‧產物流
166‧‧‧分離器流出物流
170‧‧‧第二膨脹器
172‧‧‧第二氣態排氣流
180‧‧‧第二壓縮機
182‧‧‧經壓縮之再循環流
184‧‧‧再循環之產物流
190‧‧‧第三膨脹器
192‧‧‧經膨脹之產物流
在審視以下的詳細說明及具體例的非限制性實例之圖形時，可使本揭露的前述及其他優點變得顯而易見，其中： 圖1描述包含兩個經流體連結之氣渦輪機系統及併有CO2分離之組合式低排放動力產生系統。
圖2描述圖1之組合式低排放動力產生系統的變化，其中將來自各渦輪機的排氣流在回收來自流的熱之前組合。
圖3描述圖1之組合式低排放動力產生系統的變化，其中將熱分開從各渦輪機的排氣流回收且將流在熱回收之後組合。
100‧‧‧動力產生系統
106‧‧‧第一膨脹器
108,188‧‧‧共軸
110‧‧‧第一燃燒室
112‧‧‧第一燃料流
114‧‧‧經壓縮之氧化劑
116‧‧‧第一排氣流
118‧‧‧第一壓縮機
120‧‧‧氧化劑進料
122‧‧‧第一氣態排氣流
126‧‧‧熱回收蒸汽產生器(HRSG)
130‧‧‧蒸汽
132‧‧‧經組合之排氣流
134‧‧‧冷卻單元
136‧‧‧水漏失流
140‧‧‧經冷卻之再循環流
150‧‧‧第二燃燒室
152‧‧‧第二燃料流
156‧‧‧第二排氣流
162‧‧‧分離器
164‧‧‧產物流
166‧‧‧分離器流出物流
170‧‧‧第二膨脹器
172‧‧‧第二氣態排氣流
180‧‧‧第二壓縮機
182‧‧‧經壓縮之再循環流
184‧‧‧再循環之產物流
190‧‧‧第三膨脹器
192‧‧‧經膨脹之產物流

Claims (31)

  1. 一種動力產生系統，其包含：第一壓縮機，其係經配置以接收及壓縮一或多種氧化劑，以產生經壓縮之氧化劑；第一燃燒室，其係經配置以接收及燃燒該經壓縮之氧化劑的第一部分、至少一種第一燃料及第一稀釋劑，以產生第一排氣流；第一膨脹器，其係經配置以接收來自該第一燃燒室的該第一排氣流並產生第一氣態排氣流；第二壓縮機，其係經配置以接收及壓縮經冷卻之再循環流，以產生經壓縮之再循環流；第二燃燒室，其係經配置以接收及燃燒該經壓縮之氧化劑的第二部分、至少一種第二燃料及第二稀釋劑，以產生第二排氣流；第二膨脹器，其係經配置以接收來自該第二燃燒室的該第二排氣流並產生第二氣態排氣流；熱回收蒸汽產生器，其係經配置以接收及冷卻該第一及第二氣態排氣流，以產生經組合之排氣流及蒸汽；冷卻單元，其係經配置以接收及冷卻該經組合之排氣流，並產生該經冷卻之再循環流；及分離器，其係經配置以接收及分離該經壓縮之再循環流的一部分成為分離器流出物流及分離器產物流。
  2. 根據申請專利範圍第1項之系統，其中該第一稀釋劑包含該分離器產物流的至少一部分。
  3. 根據申請專利範圍第1項之系統，其中該第二稀釋劑包含該經壓縮之再循環流的至少一部分。
  4. 根據申請專利範圍第1項之系統，其中該冷卻單元為直接接觸冷卻器。
  5. 根據申請專利範圍第1項之系統，其中該分離器產物流包含氮、氧、氬或其組合。
  6. 根據申請專利範圍第1項之系統，其中該分離器流出物流包含二氧化碳。
  7. 根據申請專利範圍第1項之系統，其中該分離器係使用選自熱碳酸鉀分離法、胺分離法、分子篩分離法、薄膜分離法、吸附動力學分離法、受控制之冷凍區分離法或其組合之分離法。
  8. 根據申請專利範圍第7項之系統，其中該分離器係使用熱碳酸鉀分離法。
  9. 根據申請專利範圍第1項之系統，其中該分離器流出物流係用於烴貯存器中以供提高油料回收。
  10. 根據申請專利範圍第1項之系統，其中該分離器產物流係用於烴貯存器中以供壓力維持。
  11. 根據申請專利範圍第1項之系統，其另外包含第三膨脹器，該第三膨脹器係經配置以接收及膨脹該分離器產物流的至少一部分。
  12. 根據申請專利範圍第11項之系統，其另外包含產物加熱單元，該產物加熱單元係經配置以接收及加熱該被引導至該第三膨脹器之該分離器產物流的部分。
  13. 根據申請專利範圍第11項之系統，其另外包含產物冷卻單元，該產物冷卻單元係經配置以接收及冷卻該經引導至該第三膨脹器之該分離器產物流的部分。
  14. 根據申請專利範圍第1項之系統，其另外包含分離器冷卻單元，該分離器冷卻單元係經配置以接收及冷卻該經引導至該分離器的該經壓縮之再循環流的部分。
  15. 一種產生動力之方法，其包含：將一或多種氧化劑在第一壓縮機中壓縮，以產生經壓縮之氧化劑；將該經壓縮之氧化劑的第一部分、至少一種第一燃料及第一稀釋劑供給至第一燃燒室；將該經壓縮之氧化劑的該第一部分及該至少一種第一燃料在該第一燃燒室中燃燒，以產生第一排氣流；將該第一排氣流在第一膨脹器中膨脹，以產生第一氣態排氣流；將經冷卻之再循環流在第二壓縮機中壓縮，以產生經壓縮之再循環流；將該經壓縮之氧化劑的第二部分、至少一種第二燃料及第二稀釋劑供給至第二燃燒室；將該經壓縮之氧化劑的該第二部分及該至少一種第二燃料在該第二燃燒室中燃燒，以產生第二排氣流；將該第二排氣流在第二膨脹器中膨脹，以產生第二氣態排氣流；從該第一及第二氣態排氣流回收熱； 將該第一及第二氣態排氣流組合，以形成經組合之排氣流；將該經組合之排氣流冷卻，以產生該經冷卻之再循環流；及將該經壓縮之再循環流的至少一部分分離，以產生流出物流及產物流。
  16. 根據申請專利範圍第15項之方法，其中熱係在一或多個熱回收蒸汽產生器中從該第一氣態排氣流、該第二氣態排氣流或兩者回收。
  17. 根據申請專利範圍第15項之方法，其中該第一及第二氣態排氣流係在從該第一及第二氣態排氣流回收熱之前組合。
  18. 根據申請專利範圍第15項之方法，其中該第一及第二氣態排氣流係在從該第一及第二氣態排氣流回收熱之後組合。
  19. 根據申請專利範圍第15項之方法，其中該第一稀釋劑包含該產物流的至少一部分。
  20. 根據申請專利範圍第15項之方法，其中該第二稀釋劑包含該經壓縮之再循環流的至少一部分。
  21. 根據申請專利範圍第15項之方法，其中該經組合之排氣流係在直接接觸冷卻器中冷卻。
  22. 根據申請專利範圍第15項之方法，其中該產物流包含氮、氧、氬或其組合。
  23. 根據申請專利範圍第15項之方法，其中該流出物 流包含二氧化碳。
  24. 根據申請專利範圍第15項之方法，其中該經壓縮之再循環流的該至少一部分係使用選自熱碳酸鉀分離法、胺分離法、分子篩分離法、薄膜分離法、吸附動力學分離法、受控制之冷凍區分離法或其組合之方法分離。
  25. 根據申請專利範圍第24項之方法，其中該經壓縮之再循環流的該至少一部分係使用熱碳酸鉀分離法分離。
  26. 根據申請專利範圍第15項之方法，其另外包含壓縮該流出物流的至少一部分，並將該流出物流注入烴貯存器中以供提高油料回收。
  27. 根據申請專利範圍第15項之方法，其另外包含將該產物流的至少一部分注入烴貯存器中以供壓力維持。
  28. 根據申請專利範圍第15項之方法，其另外包含將該產物流的至少一部分膨脹，以產生動力。
  29. 根據申請專利範圍第28項之方法，其另外包含將該產物流的該至少一部分在膨脹之前加熱。
  30. 根據申請專利範圍第28項之方法，其另外包含將該產物流的該至少一部分在膨脹之前冷卻。
  31. 根據申請專利範圍第15項之方法，其另外包含將該經壓縮之再循環流的該至少一部分在分離之前冷卻。
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