TWI579507B - 利用廢氣再循環對富集之空氣進行化學計量燃燒之系統和方法 - Google Patents
利用廢氣再循環對富集之空氣進行化學計量燃燒之系統和方法 Download PDFInfo
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- F02B47/04—Methods of operating engines involving adding non-fuel substances or anti-knock agents to combustion air, fuel, or fuel-air mixtures of engines the substances being other than water or steam only
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
- F02C6/18—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use using the waste heat of gas-turbine plants outside the plants themselves, e.g. gas-turbine power heat plants
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Description
[交互參照之相關申請案]
本申請案主張2010年7月2日申請且發明名稱為「利用廢氣再循環對富集之空氣進行化學計量燃燒」之美國專利臨時申請案第61/361,178號之優先權,該案內容係以引用方式全部併入本案。
本申請案包含與下列美國專利申請案有關之請求標的,該等相關之美國專利申請案係2010年7月2日申請且發明名稱為「控制燃料燃燒之系統和方法」的美國專利申請案第61/361,169號;2010年7月2日申請且發明名稱為「低排放三重循環發電系統和方法」的美國專利申請案第61/361,170號;2010年7月2日申請且發明名稱為「低排放三重循環發電系統和方法」的美國專利申請案第61/361,173號;2010年7月2日申請且發明名稱為「利用廢氣再循環和直接接觸式冷卻器之化學計量燃燒」的美國專利申請案第61/361,176號;2010年7月2日申請且發明名稱為「低排放發電系統和方法」的美國專利申請案第61/361,180號。
本發明之較佳體系關於複循環發電系統中之低排放發電。更特定言之,本發明之較佳體系關於燃燒燃料以增進二氧化碳(CO2)之製造和捕集的方法及設備。
此節內容係欲介紹所屬技術領域中可能與本發明之例示性實施態樣有關的各種面向。相信此節之討論內容有助於提供體系架構以利於較佳地了解本發明之特定面向。因此,應理解需以此種觀點閱讀此部分之內容,且無需承認此節之內容為先前技術。
隨著日益憂慮全球氣候變遷和排放二氧化碳(CO2)造成的衝擊問題,現已將重點擺在捕集發電廠排放的二氧化碳。基於此憂慮且結合諸多國家實施碳總量控制與排放交易管制制度(cap and trade policy)使得實施該制度的國家和其他國家及營運烴類化合物製造系統之公司的首要目標是減少二氧化碳排放。
相較於諸如燃煤發電及核能發電等其他技術而言,氣體渦輪複循環發電廠更具效率且能以相對低的成本運作。然而,捕集氣體渦輪複循環發電廠之廢氣的二氧化碳可能因數個理由而難以實行。例如,相較於必須處理的大量氣體而言,廢氣中通常含有低濃度的二氧化碳。又,將廢氣引入二氧化碳捕集系統之前,通常需要對廢氣進行額外冷卻,且於冷卻後該廢氣達水飽和,從而提高該二氧化碳捕集系統中的再沸器負荷率(reboiler duty)。其他常見因素可包括廢氣中經常含有大量且低壓的氧。所有此等因素導致氣體渦輪複循環發電廠的二氧化碳捕集成本很高。
至少一種降低複循環系統之二氧化碳排放的方法包括化學計量燃燒法和廢氣再循環法。於諸如天然氣複循環(NGCC)之習知廢氣再循環系統中,該廢氣之再循環部分係與周遭空氣混合且引入氣體渦輪之壓縮區段。天然氣複循環(NGCC)之廢氣中的典型二氧化碳濃度係約3%至4%,但利用廢氣再循環法可使二氧化碳濃度提高至高於4%。操作時,習知NGCC系統僅需要該空氣注入量之約40%的空氣以供燃料進行適當化學計量燃燒,同時剩餘60%的空氣量作為稀釋劑以緩和溫度且冷卻該廢氣達適合引入後續膨脹器中之溫度。使該廢氣之一部分再循環而提高該廢氣中的二氧化碳濃度,該部分之廢氣隨後可作為燃燒系統中的稀釋劑。
然而由於二氧化碳的分子量、比熱、馬赫數效應(Mach number effect)等等因素,且未對壓縮機區段或膨脹器區段做任何顯著修改,因此標準氣體渦輪將源自該廢氣之二氧化碳濃度限制在該氣體渦輪之壓縮區段所能承受的濃度。例如,對於標準氣體渦輪之壓縮區段的該廢氣中之二氧化碳含量限值係約20重量%之二氧化碳。
此外,典型的NGCC系統產生低壓廢氣,該低壓廢氣需藉由使該廢氣膨脹產生一部分的功率藉以萃取二氧化碳以封存或用於增強石油回收(EOR),從而降低該NGCC系統的熱效率。再者,用於二氧化碳萃取的設備係龐大並昂貴,且需要數個壓縮階段使周遭壓力氣體達到用於增進石油回收或封存所需的壓力。此等限制條件係從燃燒其他化石燃料(例如煤)伴隨產生之低壓廢氣中進行燃燒後之碳捕集的典型條件。
以上討論之所屬技術領域的需求係作為示範說明之用,而非詳盡列舉。可解決所屬技術領域中之一或多個此等需求或某些其他相關缺點的技術將對複循環發電系統中之發電有所助益。
本發明係有關用於改善發電系統之整合式系統及方法。於某些較佳體系中,本發明提供一種氣體渦輪系統,該氣體渦輪系統包含第一壓縮機、第二壓縮機、燃燒腔室和膨脹器。該第一壓縮機可經建構以接收且壓縮再循環廢氣成為經壓縮之再循環廢氣。該第二壓縮機可經建構以接收且壓縮富集之空氣以生成經壓縮之氧化劑。該燃燒腔室可經建構以接收該經壓縮之再循環廢氣和該經壓縮之氧化劑且使燃料流進行化學計量燃燒。該經壓縮之再循環廢氣係作為稀釋劑以緩和燃燒溫度。該膨脹器可經建構以接收來自該燃燒腔室的排放物,藉以生成該再循環廢氣。該膨脹器可進一步耦接該第一壓縮機以至少部分驅動該第一壓縮機。
額外或替代地,本發明提供數種發電方法。例示性方法包含:a)於主壓縮機中壓縮再循環廢氣以生成經壓縮之再循環廢氣;b)於入料壓縮機中壓縮富集之空氣以生成經壓縮之氧化劑;c)於燃燒腔室內且於該經壓縮之再循環廢氣的存在下使該經壓縮之氧化劑與燃料進行化學計量燃燒,從而生成排放氣流,其中該經壓縮之再循環廢氣係作為用於緩和該排放氣流之溫度的稀釋劑;及d)於膨脹器中膨脹該排放氣流以至少部分驅動該主壓縮機且生成該再循環廢氣並至少部分驅動該主壓縮機。
又額外或替代地,本發明提供數種整合式發電系統。例示性之整合式發電系統包含氣體渦輪系統和廢氣再循環系統兩者。該氣體渦輪系統可包含第一壓縮機、第二壓縮機、燃燒腔室和膨脹器。該第一壓縮機可經建構以接收且壓縮再循環廢氣成為經壓縮之再循環廢氣。該第二壓縮機可經建構以接收且壓縮富集之空氣以生成經壓縮之氧化劑,該富集之空氣含有介於約30重量%至約50重量%之氧濃度。該燃燒腔室可經建構以接收該經壓縮之再循環廢氣和該經壓縮之氧化劑且使燃料流進行化學計量燃燒,其中該經壓縮之再循環廢氣係作為稀釋劑以緩和燃燒溫度。該膨脹器可經建構以接收來自該燃燒腔室的排放物,藉以生成該再循環廢氣。該膨脹器可進一步耦接該第一壓縮機,且該膨脹器可經調適以至少部分驅動該第一壓縮機。該廢氣再循環系統可包含熱回收蒸汽產生器、一或多個冷卻單元和增壓壓縮機。該熱回收蒸汽產生器與蒸汽渦輪可連通地耦接。該熱回收蒸汽產生器可經建構以接收來自該膨脹器之該再循環廢氣以於該蒸汽產生器內製造能產生電力的蒸汽。該一或多個冷卻單元可經建構以冷卻自該熱回收蒸汽產生器所接收的該再循環廢氣且去除該再循環廢氣中之凝結水。該增壓壓縮機可經建構以提高該再循環廢氣之壓力且之後該再循環廢氣注入該第一壓縮機以提供該經壓縮之再循環廢氣。
於以下實施方式之段落中,係結合多個較佳實施態樣說明本發明之數個特定實施方式。然而,當下述內容係特別針對本發明之一特定實施態樣或特定用途時,此係僅單純為達示範目的而提供例示性實施態樣之描述。因此,本發明不限於下述特定實施態樣,反之,本發明包含所有落入後附申請專利範圍之精神真諦與範圍內的多種替代物、修飾例和等效物。
本案中所使用之各種用語係定義如下。若下文未定義申請專利範圍中所使用之用語,應以所屬技術領域人士回應至少一篇印刷出版刊物或經核准之專利所賦予該用語之最廣定義而界定該用語。
當用於本案中,「天然氣」一詞係指得自原油井之多成分氣體(伴生氣體)或得自地下含氣層之多成分氣體(非伴生氣體)。天然氣的組成和壓力可能顯著變化。典型的天然氣流含有作為主要成分之甲烷(CH4),即天然氣流中超過50莫耳%的成分為甲烷。天然氣流亦可含有乙烷(C2H6)、較高分子量之烴類化合物(例如,C3-C20烴類化合物)、一或多種酸性氣體(例如,硫化氫、二氧化碳)或上述化合物之任意組合。天然氣亦可含有次量的污染物,例如水、氮氣、硫化鐵、蠟、原油或上述物質之任意組合。
當用於本案中,「化學計量燃燒」之用語係指一數量之含有燃料和氧化劑之反應物的燃燒反應且藉著燃燒該等反應物而生成一數量的產物,其中該等反應物之全部量係用於形成該等產物。當用於本案中,「實質化學計量燃燒」之用語係指燃燒之燃料與氧的莫耳比介於達成化學計量比例所需氧量之約正負10%之間、或較佳介於達成化學計量比例所需氧量之約正負5%之間的燃燒反應。例如,對於甲烷而言,燃料與氧氣的化學計量比例係1:2(CH4+2O2→CO2+2H2O)。丙烷將具有燃料與氧氣為1:5的化學計量比例。另一種測量實質化學計量燃燒的方法係按所供應之氧與達成化學計量燃燒所需要之氧的比例計算,例如該比例可介於約0.9:1至約1.1:1,或更佳介於約0.95:1至約1.05:1。
當用於本案中,「流(stream)」之用語係指一數量之流體,雖然使用「流」一詞通常表示移動中的流體量(例如該流體具有流速或質量流率(mass flow rate))。然而,該用語「流」未必需要流速、質量流率或用於圈圍該流體之特定種類的導管。
本案揭示之系統和方法的實施態樣可用於產生超低排放電力及產生用於增強石油回收(EOR)及/或封存之應用的二氧化碳。在一或多個實施態樣中,富集之空氣與燃料的混合物可進行化學計量燃燒或實質化學計量燃燒且與再循環廢氣流混合。該再循環廢氣流通常含有燃燒產物(例如,二氧化碳),且該再循環廢氣流可用於作為稀釋劑
以控制、調節或緩和燃燒溫度及作為進入接續之膨脹器中的廢氣。使用富集之空氣的結果是該再循環廢氣可具有提高的二氧化碳含量,從而允許該膨脹器在相同的入料溫度及排放溫度下能以更高膨脹率運作,從而產生顯著提高的功率。
在商業用氣體渦輪中於化學計量條件或實質化學計量條件下燃燒(例如,"微富(slightly rich)"燃燒)證明有利於減少去除過多氧的費用。藉著冷卻該廢氣且使該經冷卻之廢氣流中的水凝結,可製造出二氧化碳含量相對高的廢氣流。該再循環廢氣之一部分可在密閉式布雷頓循環(closed brayton cycle)中用於緩和溫度,同時剩餘的淨化氣流可用於EOR應用,且/或於僅排放極少或不排放氧化硫(SOx)、氧化氮(NOx)及/或二氧化碳(CO2)至大氣中的情況下產生電力。此方法之結果係於三個不同循環中產生功率且製造額外的二氧化碳。
現參閱該等圖式,第1圖係根據一或多個實施態樣圖示使用複循環配置以用於發電和回收二氧化碳之例示性整合系統的概要圖。於至少一實施態樣中,該發電系統100可包括氣體渦輪系統102,該氣體渦輪系統102之特徵在於採用可產生電力之封閉式布雷頓循環。該氣體渦輪系統102可具有第一或主壓縮機104,該第一或主壓縮機104係經由軸108耦接膨脹器106。該軸108可為任何機械、電性或其他動力耦接,從而允許使用該膨脹器106所產生之機械能的一部分機械能驅動該主壓縮機104。於至少一實施態樣中,該氣體渦輪系統102可為標準氣體渦輪,其中該主壓縮機104和該膨脹器106分別形成壓縮機端和膨脹器端。然而於其他實施態樣中,該主壓縮機104及該膨脹器106可為該系統102中個別的單獨構件。
該氣體渦輪系統102亦可包括燃燒腔室110,該燃燒腔室110係經建構以燃燒經由管線112引入且與經由管線114引入之氧化劑混合的燃料。於一或多個實施態樣中,管線112中的燃料可包括任何合適的烴類化合物之氣體或液體,例如天然氣、甲烷、乙烷、石腦油(naphtha)、丁烷、丙烷、合成氣、柴油、煤油、航空燃料、煤衍生燃料、生質燃料、氧合烴類化合物原料或上述燃料之任意組合。通過管線114之氧化劑可源自第二或入料壓縮機118,該第二或入料壓縮機118係與該燃燒腔室110流體耦接且經調適以壓縮經由管線120引入的入料氧化劑。於一或多個實施態樣中,該管線120內的入料氧化劑可含有大氣空氣、富集之空氣或兩者之組合。當管線114內的氧化劑含有大氣空氣與富集之空氣的混合物時,可於該富集之空氣與該大氣空氣混合之前或混合之後藉由該入料壓縮機118壓縮該富集之空氣。該富集之空氣可含有約30重量%、約35重量%、約40重量%、約45重量%或約50重量%之總氧濃度。
該富集之空氣可源自數種來源,包括於該入料壓縮機118之上游處實施各種技術以製造該富集之空氣。例如,該富集之空氣可源自諸如薄膜分離、變壓吸附、變溫吸附之此類技術、氮氣生產機之副產物氣流及/或上述來源之組合。該富集之空氣亦可源自用於製造氮氣以保持壓力或用於其他目的之空氣分離單元(ASU),例如低溫空氣分離單元。該空氣分離單元所棄置流可富含氧且具有約50重量%至約70重量%之總氧含量。該棄置流可用於作為該富集之空氣的至少一部分,且如有需要於後續可使用未經處理的大氣空氣稀釋該棄置流以獲得用於該應用的期望氧濃度。
如以下將進一步詳細描述般,該燃燒腔室110亦可接收管線144內的經壓縮之再循環廢氣,該經壓縮之再循環廢氣包括主要含有二氧化碳和氮成分之廢氣再循環氣流。管線144內的該經壓縮之再循環廢氣可源自該主壓縮機104,且該經壓縮之再循環廢氣可經調適以藉著緩和該等燃燒產物之溫度而幫助管線114內的經壓縮之氧化劑和管線112內的燃料利於進行化學計量燃燒或實質化學計量燃燒。可理解,使該廢氣再循環可用於提高該廢氣中的二氧化碳濃度。
在管線144中的經壓縮之再循環廢氣的存在下使管線112中的燃料與管線114中的經壓縮之氧化劑燃燒而生成的產物可成為管線116中流向該膨脹器106之入口的廢氣。在至少一實施態樣中,管線112內的燃料可主要為天然氣,從而產生通過管線116的排放物或廢氣,該排放物或廢氣可包含占多個體積份量的汽化水、二氧化碳、氮氣、氧化氮(NOx)和氧化硫(SOx)。於某些實施態樣中,由於受燃燒平衡限制之故,因此管線116內的廢氣中亦可能出現管線112中之一小部分未燃燒的燃料或其他化合物。當管線116中的廢氣通過該膨脹器106而膨脹時,該廢氣產生機械功以驅動該主壓縮機104、發電機、其他設備且亦產生管線122中的氣態廢料,該氣態廢料係因管線144中經壓縮之再循環廢氣的流入而含有增高的二氧化碳含量。於某些實施方式中,該膨脹器106可經調適以產生額外的機械功,該額外的機械功可用於其他目的。
該發電系統100亦可包括廢氣再循環(EGR)系統124。在一或多個實施態樣中,該EGR系統124可包含熱回收蒸汽產生器(HRSG)126或類似裝置,且該熱回收蒸汽產生器126與蒸汽氣體渦輪128流體耦接。於至少一實施態樣中,該熱回收蒸汽產生器126與該蒸汽氣體渦輪128之組合的特徵在於形成可發電之封閉式朗肯循環(closed Rankin cycle)。結合該氣體渦輪系統102,該熱回收蒸汽產生器126和該蒸汽氣體渦輪128可形成複循環發電廠(例如天然氣複循環(NGCC)廠)的一部分。可將管線122中之氣態廢料輸送至該熱回收蒸汽產生器126以產生通過管線130之蒸汽和管線132中的經冷卻之廢氣。於一實施態樣中,可將管線130中的蒸汽送入該蒸汽氣體渦輪128以產生額外電力。
管線132中的經冷卻之廢氣可輸送至第一冷卻單元134,該第一冷卻單元134係經調適以冷卻管線132中的經冷卻之廢氣且產生經冷卻之再循環氣流140。該第一冷卻單元134可包括例如一或多個接觸式冷卻器、蛇行管冷卻器、蒸發式冷卻器或上述冷卻器之任意組合。該第一冷卻單元134亦可經調適,以經由排水流138去除任何存在於管線132內該經冷卻之廢氣中的一部分凝結水。於至少一實施態樣中,該排水流138可經由管線141而流向該熱回收蒸汽產生器(HRSG)126,以提供用於產生管線130中之額外蒸汽的水源。於其他實施態樣中,經由該排水流138回收的水可用於其他下游應用,例如用於輔助式熱交換製程。
於一或多個實施態樣中,該經冷卻之再循環氣流140可流向增壓壓縮機142。於該第一冷卻單元134中冷卻管線132內的該經冷卻之廢氣可減少於該增壓壓縮機142內壓縮該經冷卻之再循環氣流140所需的功率。與習知的扇葉或鼓風系統相反的是,該增壓壓縮機142可經建構以壓縮且提高該經冷卻之再循環氣流140之整體密度,進而將經增壓之再循環氣體引入下游管線145中,其中管線145內的該經增壓之再循環氣體具有增高的質量流動(mass flow)以達到相同的體積流量。此方式是有利的,因為該主壓縮機104係受體積流量限制,且使更多質量流動通過該主壓縮機104可產生較高的排放壓力,從而轉換成較高的橫跨該膨脹器106之壓力比。橫跨該膨脹器106產生越高的壓力比可允許達到越高的入口溫度,且因而提高膨脹器106的功率和效率。可明白此方式是有利的,因為管線116中富含二氧化碳之廢氣通常維持較高的比熱容量。
由於該主壓縮機104之吸氣壓力為該主壓縮機104的吸氣溫度之函數,所以吸氣溫度越冷,則操作該主壓縮機104以達成相同質量流動所需的功率(power)越少。因此,可隨意願地使管線145中的該經增壓之再循環氣體流向第二冷卻單元136。該第二冷卻單元136可包括例如一或多個直接接觸式冷卻器、蛇行管冷卻器、蒸發式冷卻單元或上述冷卻器之任意組合。於至少一實施態樣中,該第二冷卻單元136可作為後續冷卻器,該後續冷卻器係經調適以從管線145中的該經增壓之再循環氣體上去除至少一部分之該增壓壓縮機142所產生的壓縮熱。該第二冷卻單元136亦可經由排水流143萃取額外的凝結水。在一或多個實施態樣中,該排水流138、143可匯集成流體141且可流向或不流向熱回收蒸汽產生器126以產生流經管線130內部的額外蒸汽。
雖圖中僅圖示第一冷卻單元134和第二冷卻單元136,將理解可採用任意數目的冷卻單元以配合各種應用而不偏離本案揭示之範圍。實際上,本案亦思及使管線132內的該經冷卻之廢氣進一步流向與該廢氣再循環迴路聯結之蒸發式冷卻單元的實施態樣,例如於同時申請且發明名稱為「利用廢氣再循環及直接接觸式冷卻器之化學計量燃燒」之美國專利申請案中概要描述之冷卻單元,且該案內容中與本案揭示內容不同之部分係以引用方式併入本案。如本案所述般,該廢氣再循環系統可包含任一種經調適後可提供廢氣給該主壓縮機以將廢氣注入該燃燒腔室中的設備。
該主壓縮機104可經建構以接收且壓縮管線145內的該經增壓之再循環氣體至一額定壓力,該額定壓力係達到或高於該燃燒腔室110之壓力,從而產生管線144內的該經壓縮之再循環廢氣。可理解,於該增壓壓縮機142中壓縮該再循環廢氣之後,在該第二冷卻單元136中冷卻管線145內的該經增壓之再循環氣體可允許提高流入該主壓縮機104中之廢氣的體積質量流動。因此,此步驟可減少壓縮管線145內的該經增壓之再循環氣體達預定壓力所需的功率量。
在至少一實施態樣中,可自管線144內的該經壓縮之再循環廢氣中回收淨化氣流146,且接著於二氧化碳分離器148中處理該淨化氣流146以捕集二氧化碳而使二氧化碳以更高壓力流經管線150。管線150內的該經分離之二氧化碳可用於販賣、用於需要二氧化碳的另一製程中及/或使該二氧化碳經進一步壓縮且注入用於增強石油回收(EOR)、封存或其他目的之地面貯存槽中。由於管線112中之燃料的化學計量燃燒反應或實質化學計量燃燒反應結合源自該增壓壓縮機142之增壓壓力,使得該淨化氣流146中的二氧化碳分壓可遠高於習知氣體渦輪之廢氣中的二氧化碳分壓。因此,可使用低耗能分離法(例如,採用低耗能溶劑)進行該二氧化碳分離器148中的碳捕集。至少一種適用之溶劑係碳酸鉀(K2CO3),碳酸鉀能吸收SOx及/或NOx且使SOx及/或NOx轉換成有用的化合物,例如亞硫酸鉀(K2SO3)、硝酸鉀(KNO3)和其他簡單肥料。於同時申請且發明名稱為「低排放三重循環發電系統和方法」之美國專利申請案中可找到使用碳酸鉀進行二氧化碳捕集的例示性系統和方法,且該案內容中與本案揭示內容不同之部分係以引用方式併入本案。
實質耗盡二氧化碳且主要由氮氣所組成之殘餘氣流151亦源自該二氧化碳分離器148。於一或多個實施態樣中,可將該殘餘氣流151引入氣體膨脹器152以提供功率(power)和流經管線156的經膨脹之減壓氣體或廢氣。該膨脹器152可例如為可產生功率(power producing)之氮氣膨脹器。如圖所示,該氣體膨脹器152可隨意地透過共軸154或其他機械性、電性或其他動力耦接方式耦接該入料壓縮機118,從而允許該氣體膨脹器152所產生之功率的一部分功率驅動該主壓縮機118。然而,於該系統100開始啟動期間及/或當該氣體膨脹器152無法供應該入料壓縮機118運作所需之全部功率時的正常操作期間,可使用至少一個馬達158(例如電動馬達)與該氣體膨脹器152協同運作。例如,可合理設計該馬達158之尺寸,使得於該系統100之正常操作期間,該馬達158可經配置以補足該氣體膨脹器152無法提供的功率差額。於其他實施態樣中,該氣體膨脹器152可用於為其他應用提供功率,且該氣體膨脹器152不直接耦接該入料壓縮機118。例如,該膨脹器152所產生之功率與該壓縮機118所需之功率可能實質不匹配。於此等情況下,該膨脹器152可經調適以驅動需要較少功率的較小壓縮機或需要較多功率的較大壓縮機(圖中未顯示)。
該氣體膨脹器152可排放管線156內的經膨脹之減壓氣體,且該經膨脹之減壓氣體係主要由乾燥氮氣所組成。於至少一實施態樣中,該氣體膨脹器152、入料壓縮機118和二氧化碳分離器148之組合的特色在於提供開放式布雷頓循環或作為該發電系統100的第三功率產生構件。於同時申請且發明名稱為「低排放三重循環發電系統和方法」之美國專利申請案中可找到用於膨脹該殘餘氣流151中之氮氣的例示性系統和方法及該等系統和方法之變化型,且該案內容中與本案揭示內容不同之部分係以引用方式併入本案。
參閱第2圖,第2圖顯示根據一或多個實施態樣之使用複循環配置以用於發電和回收二氧化碳之例示性整合系統200的另一概要圖。第2圖之系統200係實質類似第1圖之系統100,且因此將不針對第2圖中使用相同元件符號表示的相同元件作詳細說明。然而第2圖之系統200可使用下游壓縮機158取代該系統100中的氣體膨脹器152,該下游壓縮機158係經建構以壓縮該殘餘氣流151且產生流經管線160的經壓縮之廢氣。於一或多個實施態樣中,管線160內的該經壓縮之廢氣可適合注入用於壓力維持用途的貯存槽中。於通常將甲烷氣體再注入烴類化合物井內以維持井壓的應用中,壓縮該殘餘氣流151可能是有利的。例如,可改將管線160內的該經增壓之氮氣注入該等烴類化合物井中,且任何殘餘的甲烷氣體可用於販售或作為相關應用中的燃料,例如可供應管線112中的燃料。
參閱第3圖,第3圖顯示根據一或多個實施態樣之使用複循環配置以用於發電和回收二氧化碳之例示性整合系統300的另一概要圖。第3圖之系統300係分別實質類似第1圖之系統100和第2圖之系統200,且因此將不針對第3圖中使用相同元件符號表示的相同元件作詳細說明。如圖所示,該系統300之特色可在於參照第1圖所述該可產生功率之氮氣膨脹器152與參照第2圖所述該用於維持壓力之下游壓縮機158所組成的混合配置。於一或多個實施態樣中,該殘餘氣流151可分流,從而使該殘餘氣流151之第一部分流向該氣體膨脹器152,且同時使該殘餘氣流151之第二部分經由管線162流向該下游壓縮機158。於至少一實施態樣中,該第一部分和該第二部分各自的體積質量流動可經操作以提供預定量及/或期望量的殘餘氣流151給該氣體膨脹器152或下游壓縮機158之任一位置以使功率產出最大化。
藉著使用富集之空氣作為管線114內的經壓縮之氧化劑且於該增壓壓縮機142中增壓該廢氣,該發電系統100可達到使該廢氣中含更高的二氧化碳濃度,從而允許達成更有效的二氧化碳分離和捕集作用。本案揭示之實施態樣可有效地使管線116內之廢氣中的二氧化碳濃度提高至介於約10重量%至約20重量%的二氧化碳濃度。為達成此等二氧化碳濃度,該燃燒腔室110可經調適以使管線112中之燃料與管線114中經壓縮之氧化劑所組成的入料混合物進行化學計量燃燒或實質化學計量燃燒,其中管線114中的該經壓縮之氧化劑包括含有約30重量%、約35重量%、約40重量%、約45重量%或約50重量%之總氧濃度的富集之空氣。
為緩和該化學計量燃燒之溫度以滿足膨脹器106之入料溫度和構件冷卻需求,可使源自管線144內該經壓縮之再循環廢氣的一部分含有高二氧化碳含量之廢氣注入該燃燒腔室110中以作為稀釋劑。因此,本發明之實施態樣可實質去除管線116內之廢氣中過量的氧,亦同時使該廢氣之二氧化碳濃度提高至約20重量%。如此,管線122內的氣態廢料可含有少於約3.0重量%之氧,或少於約1.0重量%之氧,或少於約0.1重量%之氧,或甚至少於約0.001重量%之氧。
含有高二氧化碳濃度之至少一個益處在於該膨脹器106能於相同的入料溫度和排放溫度下以較高的膨脹比運作,且從而產生更多功率。此係由於二氧化碳之熱容量比周遭空氣中之氮氣的熱容量更高之故。於一或多個實施態樣中,分別對應於約含10重量%至約20重量%之二氧化碳的再循環氣流而言,該膨脹器106之膨脹比可自約17.0提高至約20.0。使用約35重量%之氧的富集之氣體的實施態樣可用於達成含有約20重量%之二氧化碳的再循環氣流。
再循環氣體中含有更高二氧化碳濃度的其他益處包括用於分離二氧化碳的經萃取之淨化氣流146中含有更高的二氧化碳濃度。由於淨化氣流146含有增高的二氧化碳濃度,該淨化氣流146無需大量即可萃取得到所需的二氧化碳量。例如,用於操作用於分離二氧化碳之萃取動作的設備(包括該設備之管線、熱交換器、閥、吸收塔,等等)可較小。此外,增高的二氧化碳濃度可增進二氧化碳去除技術之效能,該二氧化碳去除技術包括使用低能源分離法,例如使用低耗能溶劑(less energy-intensive solvent),否則將難以支持上述低能源分離法進行。因而可巨幅降低捕集二氧化碳之資本支出。
現將討論該系統100之例示性操作的各項細節。將可理解,本案揭示任何實施態樣之各種構件中所達到或經歷的特定溫度和壓力可根據其他因素而改變,特別是可根據所使用之氧化劑的純度及/或膨脹器、壓縮機、冷卻器等等構件之特定品牌或型號而改變。因此,將可理解,本案所述之特定數據係僅用於說明目的且不應將該等特定數據視為唯一解釋。於一實施態樣中,該入料壓縮機118可提供管線114內壓力介於約280 psia至300 psia的經壓縮之氧化劑。然而於本案中亦可思及氣輪式氣體渦輪技術,該技術可產生及消耗高達約750 psia和更高的壓力。
該主壓縮機104可經建構以再循環和壓縮再循環廢氣而成為管線144中的該經壓縮之再循環廢氣,該經壓縮之再循環廢氣的額定壓力係高於或處於該燃燒腔室110之壓力,且使用該再循環廢氣之一部分廢氣作為該燃燒腔室110中的稀釋劑。由於該燃燒腔室110中所需之稀釋劑的量可根據於用於化學計量燃燒之氧化劑的純度或膨脹器106之特定型號或設計而有所不同,因此可於該膨脹器106之出口上設置一圈熱電偶及/或氧感測器(圖中未顯示)。操作時,該等熱電偶和感測器可經調適以調整並決定作為稀釋劑以使該等燃燒產物冷卻至所要求之膨脹器入料溫度所需要的廢氣體積,且亦可調整欲注入該燃燒腔室110之氧化劑的量。因此,回應藉由該等熱電偶所測得之熱需求及藉由該等氧感測器所測得之氧濃度,可操控或變動管線144中的經壓縮之再循環廢氣和管線114中的經壓縮之氧化劑的體積質量流動以符合該需求。於同時申請且發明名稱為「用於控制燃料燃燒之系統和方法」之美國專利申請案中可找到用於控制燃燒燃料所產生之廢氣組成的系統和方法之例示性實施態樣及進一步詳細描述,且該案內容中與本案揭示內容不同之部分係以引用方式併入本案。
於至少一實施態樣中,於化學計量燃燒或實質化學計量燃燒期間,橫跨該燃燒腔室110可能經歷約12psia至13psia之壓降。管線112中的燃料與管線114中的該經壓縮之氧化劑的燃燒反應可產生介於約2000℉至3000℉間之溫度和介於250psia至約300psia間之壓力。如上述,由於自管線144中的該經壓縮之再循環廢氣所獲得富含二氧化碳之廢氣具有更高質量流動和更高的比熱容量,橫跨該膨脹器106可達到更高的壓力比,從而允許達到較高的入料溫度和更多的膨脹器106之功率。
離開該膨脹器106且於管線122中之氣態廢料可表現出處於或接近周遭環境之壓力。於至少一實施態樣中,管線122中之氣態廢料具有約13-17psia之壓力。管線122中之該氣態廢料於通過該熱回收蒸汽產生器126以產生管線130中之蒸汽和管線132中經冷卻之廢氣之前,管線122中之該氣態廢料的溫度可約1225℉至約1275℉。於一或多個實施態樣中,該冷卻單元134可降低管線132內的該經冷卻之廢氣的溫度,從而產生具有介於約32℉至約120℉間之溫度的該經冷卻之再循環氣流140。可理解,此等溫度可主要根據全球特定地區之特定季節期間內的濕球溫度而波動。
根據一或多個實施態樣,該增壓壓縮機142可經建構以使該經冷卻之再循環氣流140的壓力升高至介於約17psia至約21psia之間的壓力。因此,該主壓縮機104最終接收且壓縮一具有較高密度和更高質量流動的再循環廢料,從而允許達到實質更高的排放壓力且同時維持相同或相似的壓力比。為進一步提高該再循環廢氣之密度和質量流動,隨後可於該第二冷卻單元136中進一步冷卻自該增壓壓縮機142所排出之管線145中的該經增壓之再循環氣體。於一或多個實施態樣中,該第二冷卻單元136可經建構,以於管線145中的該經增壓之再循環氣體流向該主壓縮機104之前,使管線145中該經增壓之再循環氣體的溫度降低至約105℉。
於至少一實施態樣中,自該主壓縮機104排出之管線144內的該經壓縮之再循環廢氣的溫度且從而使該淨化氣流146之溫度可約達800℉且具有約280psia之壓力。增設該增壓壓縮機142和富集之空氣的化學計量燃燒反應可提高該淨化氣流146中之二氧化碳淨化壓(purge pressure),且由於該淨化氣流146中含有較高二氧化碳分壓可導致該二氧化碳分離器148中的溶劑處理效能增高。
可藉由下述模擬實例進一步說明本發明之實施態樣。雖然該模擬實例係針對一特定實施態樣,但該模擬實例不應視為對本發明之任何特定方面上的限制。
為說明使用富集之空氣作為管線114中經壓縮之氧化劑的卓越效能,該系統100係模擬於相同周遭環境條件下以相同氣體渦輪系統102使用標準空氣且隨後使用含有約35重量%氧濃度之富集空氣的試驗。下表提供此等試驗之結果和效能評估。
應可從表一理解到,包含富集之空氣作為管線114中該經壓縮之氧化劑的實施態樣由於可使該膨脹器106具有提高的膨脹壓力比且提高通過該膨脹器106的質量流動,因而可造成提高膨脹器106之功率的結果。此外,雖然該主壓縮機104對於功率的需求可能稍有提高(此提高部分係由於去除空氣中之一部分的氮氣成分所造成),但該入料壓縮機118中所減少的空氣壓縮功率遠遠抵消該主壓縮機對功率需求的提高,從而導致所需要之總壓縮功率整體減少。可理解,由於用於達成相同氧量所需之空氣流減小,因此該入料壓縮機118所需之壓縮機功率能大幅降低。重要的是,表一顯示複循環功率輸出大幅提高,且該複循環功率輸出大幅提高在複循環效率上帶來約1.0%的提升。
以上討論之該等例示性實施態樣係僅作示範之用,但本發明可容許具有各種修飾例和替代形態。然而,亦應再次了解本發明不僅限於本案中揭示之特定實施態樣。實際上,本發明包含落入後附申請專利範圍之精神真諦和範圍內的所有替代例、修飾例和等效物。
100...發電系統
102...氣體渦輪系統
104...第一壓縮機或主壓縮機
106...膨脹器
108...軸
110...燃燒腔室
112...管線
114...管線
116...管線
118...第二壓縮機或入料壓縮機
120...管線
122...管線
124...廢氣再循環系統
126...熱回收蒸汽產生器
128...蒸汽氣體渦輪
130...管線
132...管線
134...第一冷卻單元
136...第二冷卻單元
138...排水流
140...經冷卻之再循環氣流
141...流體
142...增壓壓縮機
143...排水流
144...管線
145...管線
146...淨化氣流
148...二氧化碳分離器
150...管線
151...殘餘氣流
152...氣體膨脹器
154...共同軸
156...管線
158...馬達/下游壓縮機
160...管線
162...管線
200...系統
300...系統
於閱讀上述實施方式及較佳體系之非限制性實例的圖式後,可明白本發明之上述優點和其他優點,且該等附圖如下:
第1圖顯示根據所述之一或多個較佳體系之用於低排放發電且增進二氧化碳回收之整合系統的概要圖。
第2圖顯示根據所述之一或多個較佳體系之用於低排放發電且增進二氧化碳回收之整合系統的另一概要圖。
第3圖顯示根據所述之一或多個較佳體系之用於低排放發電且增進二氧化碳回收之整合系統的另一概要圖。
100...發電系統
102...氣體渦輪系統
104...第一壓縮機或主壓縮機
106...膨脹器
108...軸
110...燃燒腔室
112...管線
114...管線
116...管線
118...第二壓縮機或入料壓縮機
120...管線
122...管線
124...廢氣再循環系統
126...熱回收蒸汽產生器
128...蒸汽氣體渦輪
130...管線
132...管線
134...第一冷卻單元
136...第二冷卻單元
138...排水流
140...經冷卻之再循環氣流
141...流體
142...增壓壓縮機
143...排水流
144...管線
145...管線
146...淨化氣流
148...二氧化碳分離器
150、156...管線
151...殘餘氣流
152...氣體膨脹器
154...共同軸
158...馬達/下游壓縮機
Claims (18)
- 一種氣體渦輪系統,該系統包含:第一壓縮機,該第一壓縮機係經建構以僅接收且壓縮再循環廢氣成為經壓縮之再循環廢氣;第二壓縮機,該第二壓縮機係經建構以僅接收且壓縮富集之空氣以生成經壓縮之氧化劑,該富集之空氣含有介於30重量%至50重量%之氧濃度;燃燒腔室,該燃燒腔室係經建構以分別接收該經壓縮之再循環廢氣和該經壓縮之氧化劑且使燃料流進行化學計量燃燒,其中該經壓縮之再循環廢氣係作為稀釋劑以緩和燃燒溫度;及膨脹器,該膨脹器與該第一壓縮機耦接,且該膨脹器係經建構以接收來自該燃燒腔室的排放物,藉以生成該再循環廢氣且至少部分驅動該第一壓縮機。
- 如申請專利範圍第1項之系統,其中該富集之空氣係與大氣空氣混合。
- 如申請專利範圍第1項之系統,其中該富集之空氣係得自薄膜分離、變壓吸附、變溫吸附或上述之任意組合。
- 如申請專利範圍第1項之系統,其中該富集之空氣係得自空氣分離單元之棄置流。
- 如申請專利範圍第4項之系統,其中該棄置流含有介於50重量%至70重量%之氧濃度。
- 如申請專利範圍第1項之系統,其中該再循環廢氣 含有介於10重量%至20重量%之二氧化碳濃度。
- 如申請專利範圍第1項之系統,其中該燃料流係選自下列群組:天然氣、甲烷、石腦油、丁烷、丙烷、合成氣、柴油、煤油、航空燃料、煤衍生燃料、生質燃料、氧合烴類化合物原料及上述燃料之任意組合。
- 如申請專利範圍第1項之系統,該系統進一步包含淨化氣流,該淨化氣流係取自該經壓縮之再循環廢氣,且該淨化氣流係於二氧化碳分離器中經處理以產生二氧化碳氣流和實質包含氮氣之殘餘氣流。
- 一種發電之方法,該方法包含:於主壓縮機中僅壓縮再循環廢氣以生成經壓縮之再循環廢氣;於入料壓縮機中僅壓縮富集之空氣以生成經壓縮之氧化劑,該富集之空氣含有介於30重量%至50重量%之氧濃度;將該經壓縮之再循環廢氣和該經壓縮之氧化劑分別輸送至燃燒腔室;於燃燒腔室內且於該經壓縮之再循環廢氣的存在下使該經壓縮之氧化劑與燃料進行化學計量燃燒,從而生成排放氣流,其中該經壓縮之再循環廢氣係作為用於緩和該排放氣流之溫度的稀釋劑;及於膨脹器中膨脹該排放氣流以至少部分驅動該主壓縮機且生成該再循環廢氣並至少部分驅動該主壓縮機。
- 如申請專利範圍第9項之方法,該方法進一步包 含使該富集之空氣與大氣空氣混合。
- 如申請專利範圍第9項之方法,其中該再循環廢氣含有介於10重量%至20重量%之二氧化碳濃度。
- 如申請專利範圍第9項之方法,其中該富集之空氣係得自空氣分離單元之棄置流,該棄置流含有介於50重量%至70重量%之氧濃度。
- 一種整合系統,該整合系統包含:氣體渦輪系統,該氣體渦輪系統包含:第一壓縮機,該第一壓縮機係經建構以僅接收且壓縮再循環廢氣成為經壓縮之再循環廢氣;第二壓縮機,該第二壓縮機係經建構以僅接收且壓縮富集之空氣以生成經壓縮之氧化劑,該富集之空氣含有介於30重量%至50重量%之氧濃度;燃燒腔室,該燃燒腔室係經建構以分別接收該經壓縮之再循環廢氣和該經壓縮之氧化劑且使燃料流進行化學計量燃燒,其中該經壓縮之再循環廢氣係作為稀釋劑以緩和燃燒溫度;及膨脹器,該膨脹器與該第一壓縮機耦接,且該膨脹器係經建構以接收來自該燃燒腔室之排放物,以生成該再循環廢氣且至少部分驅動該第一壓縮機;及廢氣再循環系統,該廢氣再循環系統包含:熱回收蒸汽產生器,該熱回收蒸汽產生器係與蒸汽渦輪可連通地耦接,該熱回收蒸汽產生器係經建構以接收來自該膨脹器之該再循環廢氣以於該蒸汽產生器內製造能產 生電力的蒸汽;一或多個冷卻單元,該等冷卻單元係經建構以冷卻自該熱回收蒸汽產生器所接收的該再循環廢氣且去除該再循環廢氣中之凝結水;及增壓壓縮機,該增壓壓縮機係經建構以提高該再循環廢氣之壓力且之後該再循環廢氣注入該第一壓縮機,以提供該經壓縮之再循環廢氣。
- 如申請專利範圍第13項之系統,其中該增壓壓縮機使該再循環廢氣流之壓力提高至介於17 psia至21 psia之間。
- 如申請專利範圍第13項之系統,其中該再循環廢氣含有介於15重量%至20重量%之二氧化碳濃度。
- 如申請專利範圍第13項之系統,其中該富集之空氣係與大氣空氣混合。
- 如申請專利範圍第13項之系統,其中該富集之空氣係得自薄膜分離、變壓吸附、變溫吸附、空氣分離單元或上述之任意組合。
- 如申請專利範圍第17項之系統,其中該空氣分離單元含有棄置流,該棄置流含有介於50重量%至70重量%之氧濃度,該棄置流實質上提供該富集之空氣。
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JP5906555B2 (ja) | 2016-04-20 |
EA029336B1 (ru) | 2018-03-30 |
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CA2801494C (en) | 2018-04-17 |
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CA2801494A1 (en) | 2012-01-05 |
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BR112012031505A2 (pt) | 2016-11-01 |
WO2012003079A1 (en) | 2012-01-05 |
MX2012014458A (es) | 2013-02-07 |
MX354587B (es) | 2018-03-12 |
CN102959203A (zh) | 2013-03-06 |
MY160833A (en) | 2017-03-31 |
US9903316B2 (en) | 2018-02-27 |
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