TWI564476B - 使用排放氣再循環系統和直接接觸冷卻器進行之化學計量燃燒 - Google Patents

使用排放氣再循環系統和直接接觸冷卻器進行之化學計量燃燒 Download PDF

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TWI564476B
TWI564476B TW100120162A TW100120162A TWI564476B TW I564476 B TWI564476 B TW I564476B TW 100120162 A TW100120162 A TW 100120162A TW 100120162 A TW100120162 A TW 100120162A TW I564476 B TWI564476 B TW I564476B
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羅伯 戴特
希曼蘇 古塔
理查 杭汀頓
摩西斯 密塔
法蘭克林 密特利克
羅倫 史達徹
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艾克頌美孚上游研究公司
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C1/00—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid
    • F02C1/007—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid combination of cycles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
    • F02B47/00—Methods of operating engines involving adding non-fuel substances or anti-knock agents to combustion air, fuel, or fuel-air mixtures of engines
    • 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
    • F02B47/08—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 the substances including exhaust gas
    • F02B47/10—Circulation of exhaust gas in closed or semi-closed circuits, e.g. with simultaneous addition of oxygen
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Treating Waste Gases (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Gas Separation By Absorption (AREA)
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Description

使用排放氣再循環系統和直接接觸冷卻器進行之化學計量燃燒 相關申請案之交叉參考
本申請案主張在2010年7月2日以STOICHIOMETRIC COMBUSTION WITH EXHAUST GAS RECIRCULATION AND DIRECT CONTACT COOLER為標題申請之美國臨時專利申請案第61/361,176號之權益，將其全文併入本文以供參考。
本申請案包含與2010年7月2日以“Systems and Methods for Controlling Combustion of a Fuel”為標題申請之美國專利申請案第61/361,169號、2010年7月2日以“Low Emission Triple-Cycle Power Generation Systems and Methods”為標題申請之美國專利申請案第61/361,170號、2010年7月2日以“Low Emission Triple-Cycle Power Generation Systems and Methods”為標題申請之美國專利申請案第61/361,173號、2010年7月2日以“Stoichiometric Combustion of Enriched Air With Exhaust Gas Recirculation”為標題申請之美國專利申請案第61/361,178號及2010年7月2日以“Low Emission Power Generation Systems and Methods”為標題申請之美國專利申請案第61/361,180號有關之主題。
本發明的具體例係關於組合式循環動力系統中之低放射動力產生。
此章節意欲介紹本技藝的各種觀點，可將其與本發明的例示性具體例結合。咸信此討論有助於提供促使更瞭解本發明的特殊觀點之架構。據此應瞭解此章節應就此見解予以解讀，而沒必要解讀為承認先前技藝。
隨著對全球氣候變化及CO2放射衝擊的關懷增加而將重點寄託於從動力工廠的CO2捕獲。此關懷與許多國家中的總量管制與交易(cap-and-trade)策略之執行結合的此關懷使該等與其他國家以及操作烴生產系統的公司優先考慮降低CO2放射。
與其他技術(諸如煤和核能技術)比較時，氣體渦輪機組合式循環動力工廠相當有效且可以相對低的成本操作。然而，從氣體渦輪機組合式循環工廠之排放流捕獲CO2可因為許多理由而有困難。例如，與必須處理的大量氣體比較，通常有低濃度的CO2於排放流中。在引入排放流至CO2捕獲系統之前，常常亦需要額外的冷卻，且排放流可在冷卻之後以水變成飽和，藉此增加在CO2捕獲系統中之再沸器負荷。其他常見的因素可包括低壓力及在排放流中常含有的大量氧氣。所有的該等因素造成從氣體渦輪機組合式循環動力工廠的高成本之CO2捕獲。
一些降低CO2放射之方法包括使用溶劑(諸如胺)的燃料去碳化或燃燒後捕獲。然而，這兩種解決方案成本昂貴且降低動力產生效率，造成較低的動力生產，增加之燃料需求及增加之電力成本來滿足國內的動力需求。特別在氧氣、SOX及NOX組份的存在使得胺溶劑吸收的利用非常有問題。另一種方法為組合式循環中的含氧燃料(oxyfuel)氣體渦輪機(例如，於此來自氣體渦輪機布雷頓(Brayton)循環的排放熱經捕獲以製造蒸汽及生產在蘭金(Rankin)循環中的額外動力)。然而，沒有任何市售的氣體渦輪機可在此一循環中操作，且生產高純度氧氣所必需之動力顯著地降低製程的整體效率。許多研究比較了該等製程且出示各方法的一些優點。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，見於http：//www.energy.sintef.no/publ/xergi/98/3/3art-8-engelsk.htm(1998)。
用於降低CO2放射之其他方法包括化學計量排放氣再循環，諸如在天然氣組合式循環(NGCC)中。在習知的NGCC系統中，僅需要約40%之空氣進氣體積來提供適當的燃料化學計量燃燒，而其餘60%之空氣體積用於緩和溫度及冷卻排放氣，以便適合於引入後繼的膨脹器中，但亦不利地產生難以移除之過量的氧氣副產物。典型的NGCC生產低壓力排放氣，其需要一部分所生產之動力來抽取出用於封存或EOR之CO2，由此降低NGCC的熱效率。再者，用於CO2抽取的設備大且昂貴，並需要許多壓縮階段以使周圍壓力氣體達到EOR或封存所必需之壓力 。此等限制為從與其他的化石燃料(諸如煤)燃燒連結在一起的低壓力排放氣之後燃燒碳捕獲的典型限制。
在組合式循環動力產生工廠中之排放氣壓縮機的容量及效率直接受到入口溫度及再循環之排放氣的組成所影響。傳統上，排放氣係藉由與在直接接觸冷卻器中的再循環之水直接接觸而冷卻。再循環之水可以數種方法冷卻，包括使用排除熱至再循環之冷卻水中的熱交換器，使用空氣-鰭片式(air-fin)熱交換器，或藉由習知的冷卻塔的蒸發冷卻。然而，以該等方法冷卻受到周圍空氣條件所限制，尤其在較溫暖的氣候中。
在本技藝中要求的前述討論意欲為代表而未盡詳細。針對一或多項此等要求或此領域中的一些其他相關缺點之技術將有益於組合式循環動力系統中的動力產生。
本發明係指向改進動力產生系統之整合系統及方法。在一些執行中，本發明提供一種整合系統，其包含有利地整合之氣體渦輪機系統、排放氣再循環系統及CO2分離器。氣體渦輪機系統可具有燃燒室，而該燃燒室係經配置在經壓縮之再循環排放氣的存在下以化學計量燃燒經壓縮之氧化劑與燃料。經壓縮之再循環排放氣用於緩和燃燒室中之燃燒溫度。燃燒室引導排放物至膨脹器中，而該膨脹器係經配置以產生氣體排放流且至少部分驅動主壓縮機。將來自膨脹器之氣體排放流引導至具有至少一個整合之冷卻 單元的排放氣再循環系統中。該至少一個整合之冷卻單元冷卻在注入主壓縮機之前的氣體排放流，以產生經壓縮之再循環排放氣。CO2分離器係與經壓縮之再循環排放氣經由洗滌流以流體連結，且經配置以排放主要由富含氮氣的氣體所組成之殘餘流。富含氮氣的氣體可在氣體膨脹器中膨脹，以產生氮排放氣。將氮排放氣注入該至少一個整合之冷卻單元中，以冷卻氣體排放流。該至少一個整合之冷卻單元係經整合，使經由整合使用氮排放氣而增進至少一些冷卻效果。
另外或其他方面，本發明提供產生動力之方法。例示性方法包括：a)在燃燒室中及在經壓縮之再循環排放氣的存在下以化學計量燃燒經壓縮之氧化劑與燃料，藉此產生排放流，其中經壓縮之再循環排放氣充當稀釋劑用以緩和排放流之溫度；b)將排放流在膨脹器中膨脹，以至少部分驅動主壓縮機及產生氣體排放流；c)將氣體排放流引導至至少一個整合之冷卻單元中；d)在氣體排放流注入主壓縮機中之前，先將氣體排放流在該至少一個整合之冷卻單元中冷卻，以產生經壓縮之再循環排放氣；e)將一部分經壓縮之再循環排放氣經由洗滌流引導至CO2分離器中，該CO2分離器係經配置以排放主要由在氣體膨脹器中膨脹之富含氮氣的氣體所組成之殘餘流及產生氮排放氣；及f)將氮排放氣注入該至少一個整合之冷卻單元中，以冷卻氣體排放流。
又另外或其他方面，本發明系統可包括燃燒室、蒸發 冷卻塔及CO2分離器。燃燒室可經配置在經壓縮之再循環排放氣的存在下以化學計量燃燒經壓縮之氧化劑與燃料。燃燒室引導排放物至膨脹器中，而該膨脹器係經配置以產生氣體排放流且驅動主壓縮機。蒸發冷卻塔可具有第一塔和第二塔。第二塔可經配置以接收及冷卻在主壓縮機中壓縮之前的氣體排放流，以產生經壓縮之再循環排放氣。CO2分離器可與經壓縮之再循環排放氣經由洗滌流以流體連結，且經配置以排放主要由在氣體膨脹器中膨脹之富含氮氣的氣體所組成之殘餘流及產生氮排放氣，其中將氮排放氣注入第一塔中，以蒸發及冷卻冷卻水補給流，以排放冷卻之水，且其中將冷卻之水注入第二塔中，以冷卻氣體排放流。
在以下詳細的說明章節中，本發明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為本發明的特殊具體例或特殊用途所特有的，其意欲以例示為目的而已且簡單地提供例示性具體例的說明。據此，本發明不受限於以下說明的特定具體例，反之，本發明包括落在所附申請專利範圍之真實精神與範疇內的所有替代物、修改物及同等物。
如本文所使用之各種術語係定義於下。對於在申請專利範圍內所使用之術語未經定義於下文的情況，應根據在相關技藝中之人士在至少一個發行之刊物及公告的專利中對該術語的定義，給予其最廣泛的定義。
如本文所使用之術語〝化學計量燃燒〞係指具有一體積之包含燃料與氧化劑的反應物及一體積之由燃燒反應物所形成的產物之燃燒反應，其中使用整個反應物體積形成產物。如本文所使用之術語〝實質的化學計量燃燒〞係指具有燃燒燃料對氧氣之莫耳比在從化學計量比所必需之氧氣的約±10%，或更佳從化學計量比所必需之氧氣的約±5%為範圍之燃燒反應。例如，就甲烷的燃料對氧氣之化學計量比為1：2(CH4+2O2>CO2+2H2O)。丙烷將具有1：5之燃料對氧氣之化學計量比。測量實質的化學計量燃燒之另一方式為所供給的氧對化學計量燃燒所必需之氧氣的比值，諸如從約0.9：1至約1.1：1，或更佳從約0.95：1至1.05：1。
如本文所使用之術語〝流〞係指流體體積，雖然術語流的使用通常意謂流體的移動體積(例如，具有速度或質量流速)。然而，術語〝流〞不需要速度、質量流速或用於圍住該流之特殊類型的導管。
目前所揭示之系統及方法的具體例可用於生產超低放射的電力及用於增進油回收(EOR)及/或封存應用之CO2。在一或多個具體例中，可將空氣與燃料的混合物以化學計量或以實質的化學計量燃燒且與再循環之排放氣流混合。可將通常包括燃燒產物(諸如CO2)的再循環之排放氣流用作為稀釋劑，以控制、調整或以另外方式緩和燃燒及進入後繼膨脹器中的排放流之溫度。由於使用富含的空氣而使再循環之排氣流可具有增加之CO2含量，藉此允許膨脹器對相同的入口及排放物溫度在甚至較高的膨脹比下操作，藉此生產顯著增加之動力。
在化學計量條件或實質的化學計量條件下於市售的氣體渦輪機中燃燒(例如，〝略富〞燃燒)可證明是有利的，以消去移除過量氧氣的成本。又再者，略貧燃燒可進一步減少在排放流中的氧氣含量。藉由冷卻排放流及冷凝來自冷卻之排放流的水可生產相對高含量CO2的排放流。雖然一部分的再循環之排放氣可用於緩和密閉的布雷頓循環中之溫度，但是其餘的洗滌流可用於EOR應用及/或可生產電力，而只有少許或沒有任何氧化硫(SOX)、氧化氮(NOX)及/或CO2放射至大氣中。當洗滌流或其一部分導引至用於電力生產時，結果是以三個單獨的循環生產動力且製造出額外的CO2。
因為排放氣壓縮機的容量及效率直接受到再循環之排放氣的入口溫度所影響，所以可證明在壓縮之前降低再循環之排放氣的溫度是有利的。據此，本發明的具體例使用具有低相對濕度的氮通氣流作為在排放氣壓縮機之前的冷卻單元中之蒸發冷卻介質。乾氮氣可經配置以蒸發及冷卻適合於冷卻再循環之排放氣之水流，藉此將更冷的排放氣注入壓縮機中且藉由使壓縮機容量增加來增加其效率。可意識到可以數個理由來證明是有利的。例如，較低的抽氣溫度可等同較低的排放物溫度，其可降低低能量CO2分離製程所必需之冷卻。而且，額外的冷卻單元可從再循環之排放氣移除額外的水量，藉此降低在任何CO2分離系統中之再沸器負荷。
現參考圖形，圖1描述根據一或多個具體例之使用組合式循環排列的動力產生及CO2回收的例證用之整合系統100的示意圖。在至少一個具體例中，動力產生系統100可包括以動力生產密閉式布雷頓循環為特徵之氣體渦輪機系統102。氣體渦輪機系統102可具有第一或主壓縮機104，而該壓縮機係經由共用軸108或其他機械、電或其他動力連結方式與膨脹器106連結，藉此允許由膨脹器106所產生之機械能的一部分來驅動主壓縮機104。氣體渦輪機系統102可為一標準的氣體渦輪機，其中主壓縮機104及膨脹器106各自形成壓縮機端及膨脹器端。然而，在其他的具體例中，主壓縮機104及膨脹器106可為系統102中的個別化組件。
氣體渦輪機系統102亦可包括燃燒室110，而該燃燒室係經配置以燃燒經由管線112引入之與管線114中的經壓縮之氧化劑混合的燃料。在一或多個具體例中，在管線112中的燃料可包括任何適合的烴氣體或液體，諸如天然氣、甲烷、乙烷、石油腦、丁烷、丙烷、合成氣、柴油、煤油、航空燃料、煤衍生之燃料、生物燃料、氧化烴進料或其任何組合。在管線114中的經壓縮之氧化劑可從第二或入口壓縮機118取得，而該壓縮機與燃燒室110以流體連結且用於壓縮經由管線120引入之進料氧化劑。在一或多個具體例中，在管線120中的進料氧化劑可包括任何適合的含氧氣體，諸如空氣、富含氧的空氣、耗盡氧的空氣、純氧或其組合。
如下文更詳細地說明，燃燒室110亦可接收在管線144中的經壓縮之再循環排放氣，包括主要具有CO2和氮氣組份之排放氣再循環。在管線144中的經壓縮之再循環排放氣可從主壓縮機104取得，以用於藉由緩和燃燒產物之溫度而有助於促使管線114中的經壓縮之氧化劑與管線112中的燃料之化學計量或實質的化學計量燃燒。可意識到再循環排放氣可用於增加在排放氣中的CO2濃度。
在引導至膨脹器106入口之管線116中的排放氣可為在管線112中的燃料與在管線114中的經壓縮之氧化劑在管線144中的經壓縮之再循環排放氣的存在下之燃燒產物。在至少一個具體例中，在管線112中的燃料主要可為天然氣，藉此產生經由管線116的排放物或排放氣，其可包括體積部分的蒸氣水、CO2、氮氣、氧化氮(NOX)及氧化硫(SOX)。在一些具體例中，由於燃燒平衡的限制，在管線112中的少部分未燃燒之燃料或其他化合物可存在於管線116中的排放氣中。當管線116中的排放氣經過膨脹器106膨脹時，其產生驅動主壓縮機104、發電機或其他設備的機械動力，且亦生產氣體排放流122，而其具有由管線144中的經壓縮之再循環排放氣流入所致的較高CO2含量。除了主壓縮機104以外，或作為其替代物，膨脹器106亦可產生供使用之動力。例如，膨脹器106可生產電力。
動力產生系統100亦可包括排放氣再循環(EGR)系統124。在一或多個具體例中，EGR系統124可包括熱回收蒸汽產生器(HRSG)126或類似裝置，其與蒸汽氣體渦輪機128以流體連結。在至少一個具體例中，HRSG 126與蒸汽氣體渦輪機128之組合的特徵可為動力生產密閉式蘭金循環。在與氣體渦輪機系統102之組合中，HRSG 126及蒸汽氣體渦輪機128可構成組合式循環動力產生工廠的一部分，諸如天然氣組合式循環(NGCC)工廠。可將氣體排放流122引入HRSG 126中，以產生經由管線130的蒸汽及在管線132中的冷卻之排放氣。在一個具體例中，可將管線130中的蒸汽送至蒸汽氣體渦輪機128，以產生額外的電力。
可將管線132中的冷卻之排放氣送至再循環迴路中的任何各種裝置及/或設備，以返回主壓縮機104。在一些執行中及如圖1中所示，再循環迴路可包含第一冷卻單元134，而該單元用於冷卻管線132中的冷卻之排放氣及產生冷卻之再循環氣流140。第一冷卻單元134可包括例如一或多個接觸冷卻器、蛇行管冷卻器、蒸發冷卻單元或其任何組合。第一冷卻單元134亦可用於經由水壓降流138從管線132中的冷卻之排放氣移除一部分的任何冷凝水。在至少一個具體例中，水壓降流138可經由管線141導引至HRSG 126，以提供用於產生在管線130中的額外蒸汽之水源。在其他的具體例中，經由水壓降流138所回收之水可用於其他的下游應用，諸如輔助熱交換製程。
在一或多個具體例中，可將冷卻之再循環氣流140引導至增壓壓縮機142中。在第一冷卻單元134中冷卻在管線132中的冷卻之排放氣可降低在增壓壓縮機142中壓縮冷卻之再循環氣流140所必需之動力。與習知的風扇或吹風機系統相反，增壓壓縮機142可經配置以壓縮及增加冷卻之再循環氣流140之整體密度，藉此引導下游管線145中的經加壓之再循環氣，在管線145中的經加壓之再循環氣在此對相同的體積流量具有增加之質量流速。此可證明是有利的，因為主壓縮機104可受體積流量限制，且引導更多的質量流量經過主壓縮機104可造成較高的排放壓力，藉此轉變成橫跨膨脹器106之較高的壓力比。橫跨膨脹器106所產生之較高的壓力比可允許較高的入口溫度，且因此增加膨脹器106動力及效率。可意識到此可證明是有利的，因為在管線116中之富含CO2的排放氣通常維持較高的比熱容量。
因為主壓縮機104的抽氣壓力隨著其抽氣溫度而變化，所以對相同的質量流量而言，冷卻器抽氣溫度要求較低的動力來操作主壓縮機104。因此，可將管線145中的經加壓之再循環氣隨意地引導至第二冷卻單元136中。第二冷卻單元136可包括例如一或多個直接接觸冷卻器、蛇行管冷卻器、蒸發冷卻單元或其任何組合。在至少一個具體例中，第二冷卻單元136可用作為後冷卻器，用於移除由增壓壓縮機142產生於管線145中的經加壓之再循環氣的壓縮熱之至少一部分。第二冷卻單元136亦可經由水壓降流143抽取出額外的冷凝水。在一或多個具體例中，水壓降流138、143可會聚成流141，且可或可不導引至HRSG 126，以產生經由管線130的額外蒸汽。在第二冷卻單元136中進行冷卻之後，可將管線145中的經加壓之再循環氣引導至第三冷卻單元200中。雖然在本文僅描述第一、第二及第三冷卻單元134、136、200，但是應意識到可以不違背本發明的範疇而使用任何數量的冷卻單元，以適應於各種應用。例如，可於一些具體例中以單一個冷卻單元執行。
如下文更詳細地說明，與第一及第二冷卻單元一樣，第三冷卻單元200可為蒸發冷卻單元，而該單元係經配置以進一步降低在經由流214注入主壓縮機104之前於管線145中的經加壓之再循環氣的溫度。然而，在其他的具體例中，一或多個冷卻單元134、136、200可為不違背本發明範疇的機械冷卻系統。主壓縮機104可經配置以壓縮從第三冷卻單元200所接收之管線214中的經加壓之再循環氣至在或高於燃燒室壓力之表稱壓力，藉此產生在管線144中的經壓縮之再循環氣。可意識到在增壓壓縮機142中壓縮之後，在第二及第三冷卻單元136、200二者中冷卻在管線145中的經加壓之再循環氣可增加至主壓縮機104中之排放氣的體積質量流量。因此，此可減少壓縮在管線145中的經加壓之再循環氣至預定壓力所必需之動力量。
雖然圖1例證在排放氣再循環迴路中的三個冷卻單元及一增壓壓縮機，但是應瞭解每個該等單元均適合於降低在管線132中的冷卻之排放氣的質量流速。如上所述，降低質量流速(諸如以增壓壓縮機)與同時降低溫度是有利的。本發明係關於在動力產生系統100內的整合，以增進在排放氣再循環迴路中的排放氣之冷卻，在一些執行中，該整合可簡化排放氣再循環迴路至HSRG系統126與主壓縮機104之間的單一個冷卻單元，如本文進一步所述。
在至少一個具體例中，洗滌流146可從管線144中的經壓縮之再循環氣回收及接著在CO2分離器148中處理，以升壓下經由管線150捕獲CO2。在管線150中的經分離之CO2可供出售，用於需要CO2的其他製程中，及/或進一步壓縮及注入地面儲庫中以用於增進油回收(EOR)、封存或其他目的。因為與排放氣再循環系統124上的裝置組合之管線112中的燃料之化學計量或實質的化學計量燃燒，所以洗滌流146中的CO2分壓可比習知的氣體渦輪機排放流中之CO2分壓還更高。結果在CO2分離器148中的碳捕獲可使用低能量分離法進行，諸如低能量加強溶劑。至少一種適合的溶劑為碳酸鉀(K2CO3)，其吸收SOX及/或NOX，且將該等轉化成有用的化合物，諸如亞硫酸鉀(K2SO3)、硝酸鉀(KNO3)及其他簡單的肥料。使用碳酸鉀捕獲CO2之例示性系統及方法可見於同時申請之以“Low Emission Triple-Cycle Power Generation Systems and Methods”為標題之美國專利申請案中，將其與本發明不一致的內容併入本文以供參考。
基本上耗盡CO且主要由氮氣所組成之殘餘流151亦可從CO2分離器148取得。在一或多個具體例中，可將殘餘流151引入氣體膨脹器152中，以提供動力及經由管線156的經膨脹之洩壓氣。膨脹器152可為例如產生動力的氮氣膨脹器。如所述，氣體膨脹器152可隨意地與入口壓縮機118經過共用軸154或其他機械、電或其他動力連結方式連結，藉此使氣體膨脹器152所產生之動力的一部分驅動入口壓縮機118。然而，在其他的具體例中，氣體膨脹器152可用於提供動力至其他應用，且不與化學計量壓縮機118直接連結。例如，在由膨脹器152所產生之動力與壓縮機118的需求之間可能實質上不協調。在此等情況中，膨脹器152可能用於驅動要求較少動力之較小的壓縮機(未顯示)。或者，膨脹器可能用於驅動要求較高動力之較大的壓縮機。
主要由乾氮氣所組成之管線156中的經膨脹之洩壓氣可從氣體膨脹器152排放。如下文更詳細地說明，所得乾氮氣可助於促使在第三冷卻單元200中的水流蒸發及冷卻，以藉此冷卻在管線145中的經加壓之再循環氣。在至少一個具體例中，氣體膨脹器152、入口壓縮機118與CO2分離器之組合的特徵可為系統100的開放式布雷頓循環或第三動力生產組件。
如本文所述之動力產生系統100(特別具有來自增壓壓縮機142增加之排放氣的排放加壓)可經執行以達成在排放氣中較高的CO2濃度，藉此允許更有效的CO2分離及捕獲。例如，本文所揭示之具體例可以純甲烷燃料有效地增加排放氣排放流中的CO2濃度至約10體積%，或以更富含的氣體增加至甚至更高的CO2濃度。為了達到此濃度增加，燃燒室110可用於化學計量燃燒在管線112中的燃料與在管線114中的經壓縮之氧化劑的進料混合物。為了緩和化學計量燃燒之溫度以符合膨脹器106入口溫度及組件冷卻需求，可將從管線144中的經壓縮之再循環氣取得之排放氣的一部分注入燃燒室110中作為稀釋劑。與以過量空氣或氧化劑引入燃燒室中來緩和溫度之習知的慣例比較，再循環之排放氣的使用顯著地減少排出燃燒室110的氧氣量。因此，本發明的具體例基本上可消去排放氣的任何過量氧氣，同時增加排放氣的CO2組成。氣體排放流122本身可具有少於約3.0體積%之氧氣，或少於約1.0體積%之氧氣，或少於約0.1體積%之氧氣，或甚至少於約0.001體積%之氧氣。
現將討論系統100之例示性操作的詳細說明。經意識到本文所揭示之具體例中之任一者的各種組件中所達成或經歷之特定溫度及壓力可取決於所使用之氧化劑純度及/或膨脹器、壓縮機、冷卻器等之特殊樣式及/或型式的其他因素而改變。據此，應意識到本文所述之特殊數據僅以例證為目的且不應被理解為其唯一的解釋。例如，在本文所述的一個具體例中，入口壓縮機118可經配置以提供在管線114中的經壓縮之氧化劑在介於約280 psia至約300 psia之範圍內的壓力。然而，在本文亦涵蓋航空級(aeroderivative)氣體渦輪機技術，其可生產及消耗至多約750 psia及更高的壓力。
主壓縮機104可經配置在表稱壓力高於或在燃燒室110壓力之壓力下將再循環之排放氣再循環及壓縮至管線144中的經壓縮之再循環氣，且使用該再循環之排放氣的一部分作為燃燒室110中的稀釋劑。因為在燃燒室110中所必要之稀釋劑量可取決於化學計量燃燒所使用之氧化劑純度或膨脹器106之特殊型式或設計而定，所以可設置與燃燒室及/或膨脹器聯合的熱電偶環及/或氧感測器環(未顯示)。例如，可將熱電偶及/或氧感測器設置在燃燒室110出口上、膨脹器106入口上及/或膨脹器106出口上。在操作時，熱電偶及感測器可用於測定一或多種流之組成及/或溫度，以用於測定冷卻燃燒產物至所需的膨脹器入口溫度所必需之作為稀釋劑的排放氣的體積。另外或其他方面，熱電偶及感測器可用於測定待注入燃燒室110中的氧化劑量。因此，可以回應以熱電偶所偵測之熱需求及氧感測器所偵測之氧水平來操縱或控制在管線144中的經壓縮之再循環氣的體積質量流量及/或在管線114中的經壓縮之氧化劑，以符合要求。體積質量流速可經由任何適合的流量控制系統控制，該系統可與熱電偶及/或氧感測器以電連通。
在至少一個具體例中，在化學計量或實質的化學計量期間，橫跨燃燒室110可經歷約12-13 psia之壓力降。在管線112中的燃料與在管線114中的經壓縮之氧化劑的燃燒可產生介於約2000℉與約3000℉之溫度及從250 psia至約300 psia為範圍之壓力。因為從管線144中的經壓縮之再循環氣所取得的富含CO2的排放氣之增加的質量流量及較高的比熱容量，所以橫跨膨脹器106可達成較高的壓力比，藉此允許較高的入口溫度及增加之膨脹器106動力。
排出膨脹器106的氣體排放流122可展現在或接近周圍壓力之壓力。在至少一個具體例中，氣體排放流122可具有約13-17 psia之壓力。在通過HRSG 126之前，氣體排放流122之溫度可為約1225℉至約1275℉，以產生在管線130中的蒸汽及在管線132中的經冷卻之排放氣。
以下數個段落說明在圖1中所顯示之例示性執行。如上所述，圖1例證與排放氣再循環迴路聯合之多重裝置，以例證各種可能的組合。然而，應瞭解本文所述之本發明不需要所有的此等元件的組合，且以下列的申請專利範圍及/或主張本申請案之優先權的任何後續申請案之申請專利範圍定義。例如，雖然在圖1中例證多重冷卻單元，但是應瞭解利用與氮通氣流聯合之冷卻劑的直接接觸冷卻單元(下文以冷卻單元200說明)可憑藉單一個冷卻單元而提供足夠的冷卻。在一些執行中，冷卻單元200可提供足夠的冷卻，亦提供增壓壓縮機的優點。
繼續圖1之例示性執行的討論，在一或多個具體例中，冷卻單元134可降低管線132中的經冷卻之排放氣的溫度，藉此產生具有介於約32℉與約120℉之溫度的經冷卻之再循環氣流140。可意識到此等溫度主要可取決於地球的特定地區之特殊季節期間的濕球溫度而變動。
根據一或多個具體例，增壓壓縮機142可經配置以升高經冷卻之再循環氣流140之壓力至從約17 psia至約21 psia為範圍之壓力。除了使用冷卻單元以外，以增壓壓縮機所增加之壓縮為提供具有較高的密度及增加之質量流量的再循環之排放氣至主壓縮機104的額外方法，藉此允許實質上較高的排放壓力，同時維持相同或類似的壓力比。為了進一步增加排放氣的密度及質量流量，接著可將從增壓壓縮機142所排放之管線145中的經加壓之再循環氣在第二及第三冷卻單元136、200中進一步冷卻。在一或多個具體例中，第二冷卻單元136可經配置以降低在管線145中的經加壓之再循環氣的溫度至約105℉，然後引導至第三冷卻單元200中。如下文更詳細地討論，第三冷卻單元200可經配置以降低在管線145中的經加壓之再循環氣的溫度至低於約100℉之溫度。
在至少一個具體例中，從主壓縮機104及洗滌流146所排放的經壓縮之在管線144中之再循環氣的溫度可為約800℉，具有約280 psia之壓力。可意識到增壓壓縮機142及/或一或多個冷卻單元的添加可增加在洗滌流管線146中的CO2洗滌壓力，而由於較高的CO2分壓，可導致在CO2分離器148中的溶劑處理性能被改良。在一個具體例中，在CO2分離器148中的氣體處理法過程能需要使洗滌流146的溫度冷卻至約250℉-300℉。為了達成此冷卻，洗滌流146可通往熱交換器158，諸如交叉交換的熱交換器。從CO2分離器148中的洗滌流146抽取出CO2可留下在或接近洗滌流146的升壓及約150℉之溫度的飽和之富含氮氣的殘餘流151。熱交換器158可與如例證之殘餘流151連結或與整合系統中的其他物流或設備連結。當與殘餘流151連結時，可將殘餘流加熱，以增加從氣體膨脹器152可獲得的動力。
如上所述，殘餘流151中的氮氣，在後續膨脹成管線156中的經膨脹之洩壓氣，接著可用於蒸發及冷卻水，而該水經配置以冷卻待注入第三冷卻單元200中之管線145中的經加壓之再循環氣，該冷卻單元可為排放氣再循環迴路中唯一的冷卻單元。作為蒸發冷卻觸媒的氮氣應該儘可能乾燥。據此，可將殘餘流151引導經過經配置以冷卻殘餘流151之第四冷卻單元160或冷凝器中，藉此冷凝及經由管線162抽取出額外一部分的水。在一或多個具體例中，第四冷卻單元160可為以標準的冷卻水冷卻之直接接觸冷卻器，以降低殘餘流151的溫度至約105℉。在其他的具體例中，第四冷卻單元160可為蛇行管冷卻器或直式熱交換器。所得殘餘流151的水含量可為約0.1重量%至約0.5重量%。在一個具體例中，經由流162所移除之水可導引至HRSG 126，以產生額外的蒸汽。在其他的具體例中，在流162中的水可經處理且用作為農業用水或去礦質水。
乾氮氣可經由流164從第四冷卻單元160排放。在一個具體例中，與冷卻洗滌流146有關聯的熱能係經由熱交換器158抽取出，而該熱能可與乾氮氣流164以流體連結且經配置以再加熱在膨脹之前的氮氣。再加熱氮氣可產生經加熱之乾氮氣流166，其具有從約750℉至約790℉為範圍之溫度及約270-280 psia之壓力。在其中熱交換器158為氣體/氣體熱交換器的具體例中，在洗滌流146與乾氮氣流164之間存在有〝擠壓點(pinch point)〞溫度差異，其中乾氮氣流164通常比洗滌流146的溫度低約25℉。
在一或多個具體例中，經加熱之乾氮氣流166接著可經過氣體膨脹器152膨脹，且隨意地發動化學計量的入口壓縮機118，如上所述。據此，在熱交換器158中的交叉交換熱可經配置以捕獲從主壓縮機104所取得的大量壓縮能量，且使用該能量以使從氣體膨脹器152所抽取之動力達到最大。在至少一個具體例中，氣體膨脹器152排放在或接近大氣壓力及具有從約100℉至約105℉為範圍之溫度的管線156中的經膨脹之洩壓氮氣。可意識到在管線156中的經膨脹之洩壓氮氣的所得溫度通常可隨著排放氣之組成、洗滌氣146之溫度及在氣體膨脹器152中膨脹之前的乾氮氣流164之壓力而變化。
因為可從第四冷卻單元160中的殘餘流151移除可測量的水量，所以降低之質量流量接著在氣體膨脹器152中膨脹，因而造成動力生產減低。因此，在系統100的啟動期間及正常的操作期間，當氣體膨脹器152不能供給操作入口壓縮機118所有必需之動力時，可將至少一個馬達168(諸如電動馬達)與氣體膨脹器152以協乘方式使用。例如，可靈敏地估算出馬達168，使得馬達168可經配置在系統400的正常操作期間供給來自氣體膨脹器152不足量的動力。另外或其他方面，在氣體渦輪機152生產比入口壓縮機118所必要之動力更多的動力時，馬達168可經配置作為可轉變成發電機的馬達/發電機。
膨脹在殘餘流151中的氮氣之例證系統與方法及其變化可見於同時申請之以“Low Emission Triple-Cycle Power Generation Systems and Methods”為標題之美國專利申請案中，將其與本發明不一致的內容併入本文以供參考。
現參考圖2，該圖描述第三冷卻單元200之示意圖，如圖1中所例證。如上述所討論，所例證之第三冷卻單元200可為排放氣再循環迴路中所提供的唯一單元。另外或其他方面，第三冷卻單元200及設備的其他配件(諸如那些在圖1中所例證之配件中之一或多者)可以任何適合的排列方式配置，使得第三冷卻單元200實際上按順序為第一(或第二或其他)而不是第三冷卻單元。據此，應瞭解〝第三〞的序數命名係參考圖1的特定執行，且沒必要將圖2的冷卻單元200之特性當作系統中的第三冷卻單元來執行，反之可設置在排放氣再循環迴路中之任何適合的位置上。
在一或多個具體例中，冷卻單元200可包括與第二塔204以流體連結之第一塔202。在一或多個具體例中，第一塔202可為蒸發冷卻塔，及第二塔204可為直接接觸冷卻塔。第一塔202可經配置以接收來自氣體膨脹器152(圖1)之管線156中的經膨脹之洩壓氮氣。在一個具體例中，將管線156中的經膨脹之洩壓氮氣在或接近於第一塔202的底部注入，且經過塔上升，直到其在或接近於頂端經由氮氣出口流206排放為止。在至少一個具體例中，氮氣出口流206可排放其內容物至大氣中或以惰性氣體銷售。在其他的具體例中，在流206中的氮氣可經加壓而用於壓力維持或供EOR應用。
因為管線156中的經膨脹之洩壓氮氣可在或接近大氣壓力下，所以第一塔202可適合於在或接近大氣壓力下操作。當氮氣於第一塔202升高時，可將管線208中的水或冷卻水補給流在或接近於第一塔202頂端注入。在一或多個具體例中，在管線208中的冷卻水補給流可從地區性水體(諸如湖、河或海洋)獲得。據此，在管線208中的冷卻水補給流可取決於系統100所在之特殊地理區域的年度時間及周圍溫度而以不同的溫度注入，但是大部分有可能介於約50℉與約100℉之間。當水於第一塔202下降時，一部分的水因為吸收來自乾氮氣的熱能而蒸發，藉此冷卻水，及經由流210排放經冷卻之水。將蒸發之水與氮氣一起收集，藉此形成經由管線206排放之飽和氮氣。取決於管線206中的氮氣流之意欲用途，其中的水蒸氣可經由任何適合的方法移除。
第二塔204可經配置以在或接近於其頂端經接收冷卻之水流210。如所述，第二塔204亦可在或接近於其底部接收從第二冷卻單元136(圖1)所排放之管線145中的經加壓之再循環氣。在管線145中的經加壓之再循環氣的例證為排放氣再循環迴路中的任何排放氣流之代表。因為經加壓之再循環流145可在從約17 psia至約21 psia為範圍之壓力下注入，如上文所討論，所以可將經冷卻之水流210使用至少一種幫浦212或類似機構在適當時對應地加壓。當經冷卻之水流210及在管線145中的經加壓之再循環氣流過第二塔204時，在管線145中的經加壓之再循環氣冷卻且最終經由流214排出，接著引導至主壓縮機104(圖1)之抽氣。在一些執行中，塔204可包括多重階段或接觸表面，以增進再循環流145與經冷卻之水流210之間的交互作用。另外或其他方面，可依所欲，可使用串聯或並聯的多重塔，以取代第一塔202、第二塔204或二者。
在通常比管線210中的水更溫熱之溫度下的冷卻水返回流經由管線216排出第二塔204。可意識到冷卻在管線145中的經加壓之再循環流可造成從管線145中的經加壓之再循環氣取得更多冷凝水。此冷凝之水可經收集且與管線216中的冷卻水返回流一起排放，藉此使管線145中的經加壓之再循環氣甚至更乾，並經由流214排出。在至少一個具體例中，冷卻水返回流可經由管線208而再導引及再引入第一塔中。然而，在其他的具體例中，冷卻水返回流可無害地排放至地區性水體中或用作為灌溉用水。
如上述有關圖1的討論，在引入第三冷卻單元200中之前，可將管線145中的經加壓之再循環氣在第二冷卻單元136(圖1)中事先冷卻至約105℉之溫度。第三冷卻單元200中之管線145中的經加壓之再循環氣所經歷之整體冷卻量可取決於來自流210的經冷卻之水流經第二塔204的流速而定。
本發明的具體例可以下列的模擬實例進一步說明。雖然模擬實例係指向特定的具體例，但是不將彼等看成是以任何特定觀點來限制本發明。下表1提供例證之流210中的水流速及其對第三冷卻單元200中之冷卻過程的作用。
從表1應明白當管線210中的水流速增加時，直接由於增加之水量的熱轉移熱而使經由管線206的氮氣流之出口溫度亦增加。在管線210中的水流速增加同樣地造成管線210中的水出口之溫度增加。結果經由管線214排出的經加壓之再循環氣相對於管線210中的水流速增加而降低溫度。可意識到許多變數可影響經由管線214排出的經加壓之再循環氣的溫度，包括但不限於由管線156進料的氮排放氣之溫度、在管線208中的冷卻水補給流之溫度、在塔中的階段配置及數量等。在至少一個具體例中，可將在約80℉至約85℉之溫度之管線208中的冷卻水補給流注入第一塔202中。
下表2提供其中使用冷卻單元200(諸如本文所述之蒸發冷卻單元)的系統與沒有此一冷卻單元200的系統之間的性能比較。
從表2應明白包括循環入口冷卻的具體例(諸如使用第三冷卻單元200)可增加組合式循環動力輸出。雖然可 能經歷從氮氣膨脹器降低之動力輸出，但是其降低由增加之氣體渦輪機淨動力(亦即膨脹器106)予以更多的補償，其轉變成CO2洗滌壓力的增加(亦即主壓縮機104排放壓力)。此外，整體組合式循環動力輸出可藉由執行如本文所述之入口冷卻而增加約0.6%之lhv(較低的加熱值)。
本發明亦涵蓋使用機械冷卻系統(未顯示)作為第三冷卻單元200，以取代本文所述之蒸發冷卻單元。雖然主壓縮機104的總需求之壓縮動力可使用機械冷卻系統適當地降低，但是可對應地降低經過主壓縮機104的質量流量，其會不利地影響所生產之動力。在主壓縮機104動力降低與膨脹器106動力生產之間的取捨必須就最優的製程循環性能予以考慮。而且，額外的冷卻設備之成本應就成本-溢價解決方案予以考慮。
雖然本發明可容許各種修改及替代形式，但是上述討論之例示性實例僅以實例方式顯示。然而，應再瞭解本發明不意欲受到本文所揭示之特殊具體例的限制。事實上，本發明包括落在所附申請專利範圍的真實精神與範疇內的所有替代物、修改物及均等物。
100．．．整合系統
102．．．氣體渦輪機系統
104．．．主壓縮機
106．．．膨脹器
108．．．共用軸
110．．．燃燒室
112．．．燃料
114．．．經壓縮之氧化劑
116．．．排放氣
118．．．入口壓縮機
120．．．進料氧化劑
122．．．氣體排放流
124．．．排放氣再循環系統
126．．．熱回收蒸汽產生器
128．．．蒸汽氣體渦輪機
130．．．蒸汽
132．．．冷卻之排放氣
134．．．第一冷卻單元
136．．．第二冷卻單元
138．．．水壓降流
140．．．冷卻之再循環氣流
141．．．流
142．．．增壓壓縮機
143．．．水壓降流
144．．．經壓縮之再循環排放氣
145．．．經加壓之再循環氣
146．．．洗滌流
148．．．CO2分離器
150．．．經分離之CO2
151．．．殘餘流
152．．．氣體膨脹器
154．．．共用軸
156．．．經膨脹之洩壓氣
158．．．熱交換器
160．．．第四冷卻單元
162．．．水流
164．．．乾氮氣流
166．．．經加熱之乾氮氣流
168．．．馬達
200．．．第三冷卻單元
202．．．第一塔
204．．．第二塔
206．．．氮氣出口流
208．．．冷卻水補給流
210．．．經冷卻之水流
212．．．幫浦
214．．．流，管線
216．．．冷卻水返回流
本發明的前述及其他優點可在檢視以下的詳細說明及具體例的非限制性實例之圖式時變得顯而易見，其中：圖1描述根據本發明的一或多個具體例之用於低放射動力產生及增進CO2回收之例證用整合系統。
圖2描述根據本發明的一或多個具體例之用於冷卻在壓縮之前的排放氣之例證用冷卻單元。
100．．．整合系統
102．．．氣體渦輪機系統
104．．．主壓縮機
106．．．膨脹器
108．．．共用軸
110．．．燃燒室
112．．．燃料
114．．．經壓縮之氧化劑
116．．．排放氣
118．．．入口壓縮機
120．．．進料氧化劑
122．．．氣體排放流
124．．．排放氣再循環系統
126．．．熱回收蒸汽產生器
128．．．蒸汽氣體渦輪機
130．．．蒸汽
132．．．冷卻之排放氣
134．．．第一冷卻單元
136．．．第二冷卻單元
138．．．水壓降流
140．．．冷卻之再循環氣流
141．．．流
142．．．增壓壓縮機
143．．．水壓降流
144．．．經壓縮之再循環排放氣
145．．．經加壓之再循環氣
146．．．洗滌流
148．．．CO2分離器
150．．．經分離之CO2
151．．．殘餘流
152．．．氣體膨脹器
154．．．共用軸
156．．．經膨脹之洩壓氣
158．．．熱交換器
160．．．第四冷卻單元
162．．．水流
164．．．乾氮氣流
166．．．經加熱之乾氮氣流
168．．．馬達

Claims (21)

  1. 一種整合系統，其包含：具有燃燒室之氣體渦輪機系統，而該燃燒室係經配置在經壓縮之再循環排放氣的存在下以化學計量燃燒經壓縮之氧化劑與燃料，其中該經壓縮之再循環排放氣用於緩和燃燒室中之燃燒溫度，且燃燒室引導排放物至膨脹器中，而該膨脹器係經配置以產生氣體排放流且至少部分驅動主壓縮機；具有至少一個整合之冷卻單元的排放氣再循環系統，其中該至少一個整合之冷卻單元冷卻在注入主壓縮機之前的氣體排放流，以產生經壓縮之再循環排放氣；及CO2分離器，其與經壓縮之再循環排放氣經由洗滌流以流體連結，且經配置以排放主要由在氣體膨脹器中膨脹之富含氮氣的氣體所組成之殘餘流及產生氮排放氣，其中將該氮排放氣注入至少一個整合之冷卻單元中，以冷卻該氣體排放流。
  2. 根據申請專利範圍第1項之系統，其進一步包含至少一個額外的冷卻單元，其中該額外的冷卻單元與至少一個整合之冷卻單元以流體連結，且其中該額外的冷卻單元冷卻氣體排放流至約105℉之溫度。
  3. 根據申請專利範圍第1項之系統，其進一步包含殘餘流冷卻單元，而該冷卻單元與殘餘流以流體連結，且經配置以降低殘餘流之溫度及從該殘餘流抽取出冷凝之水。
  4. 根據申請專利範圍第3項之系統，其中該至少一個整合之冷卻單元為蒸發冷卻單元，而該蒸發冷卻單元包含：第一塔，而該塔係經配置以接收氮排放氣及冷卻水補給流，其中該氮排放氣蒸發一部分的冷卻水補給流，以冷卻該冷卻水補給流及產生冷卻之排放水；及第二塔，而該塔係經配置以接收冷卻之排放水及氣體排放流，其中在該冷卻之排放水與該氣體排放流之間的交互作用冷卻該氣體排放流。
  5. 根據申請專利範圍第4項之系統，其中該至少一個整合之冷卻單元降低經加壓之再循環流的溫度至低於約100℉。
  6. 根據申請專利範圍第4項之系統，其中該冷卻之水在引入第二塔之前以幫浦加壓。
  7. 根據申請專利範圍第4項之系統，其中該第二塔進一步經配置以從該經加壓之再循環流冷凝及抽取出水量。
  8. 根據申請專利範圍第1項之系統，其進一步包含熱交換器，而該熱交換器與洗滌流以流體連結，且經配置以降低在引入CO2分離器之前的洗滌流之溫度。
  9. 根據申請專利範圍第1項之系統，其進一步包含增壓壓縮機，而該壓縮機適合於增加在注入主壓縮機之前的氣體排放流之壓力至介於約17psia與約21psia之間的壓力。
  10. 一種產生動力之方法，其包含：將經壓縮之氧化劑與燃料在燃燒室中及在經壓縮之再循環排放氣的存在下以化學計量燃燒，藉此產生排放流，其中該經壓縮之再循環排放氣充當稀釋劑用的以緩和排放流之溫度；將該排放流在膨脹器中膨脹，以至少部分驅動主壓縮機及產生氣體排放流；將該氣體排放流引導至至少一個整合之冷卻單元中；在該氣體排放流注入該主壓縮機之前，先將該氣體排放流在該至少一個整合之冷卻單元中冷卻，以產生經壓縮之再循環排放氣；將一部分該經壓縮之再循環排放氣經由洗滌流引導至CO2分離器中，該CO2分離器係經配置以排放主要由在氣體膨脹器中膨脹之富含氮氣的氣體所組成之殘餘流及產生氮排放氣，及將該氮排放氣注入該至少一個整合之冷卻單元中，以冷卻該氣體排放流。
  11. 根據申請專利範圍第10項之方法，其進一步包含將經加壓之再循環氣在設置於最後的整合之冷卻單元之前的至少一個預冷卻單元中冷卻至約105℉之溫度，其中該至少一個預冷卻單元與最後的整合之冷卻單元以流體連結。
  12. 根據申請專利範圍第10項之方法，其進一步包含： 將該殘餘流以殘餘流冷卻單元冷卻，該冷卻單元與該CO2分離器以流體連結；及從殘餘流抽取出冷凝之水。
  13. 根據申請專利範圍第12項之方法，其進一步包含：在該至少一個整合之冷卻單元的第一塔中接收該氮排放氣及冷卻水補給流；將一部分的該冷卻水補給流蒸發，以冷卻該冷卻水補給流，及產生冷卻之排放水；在該至少一個整合之冷卻單元的第二塔中接收該冷卻之排放水及該氣體排放流；將該氣體排放流以該冷卻之排放水冷卻至低於約100℉之溫度。
  14. 根據申請專利範圍第13項之方法，其進一步包含將該冷卻之排放水在引入該第二塔之前以幫浦加壓。
  15. 根據申請專利範圍第13項之方法，其進一步包含在第二塔中從該經加壓之再循環流冷凝及抽取出水量。
  16. 根據申請專利範圍第10項之方法，其進一步包含在熱交換器中降低該洗滌流之溫度，而該熱交換器與該洗滌流以流體連結，且經配置以降低在引入CO2分離器之前的該洗滌流之溫度。
  17. 一種組合式循環動力產生系統，其包含：燃燒室，而該燃燒室係經配置在經壓縮之再循環排放氣的存在下以化學計量燃燒經壓縮之氧化劑與燃料，其中 該燃燒室引導排放流至膨脹器中，而該膨脹器經配置以產生氣體排放流及驅動主壓縮機；具有第一塔和第二塔的蒸發冷卻塔，其中該第二塔係經配置以接收及冷卻在該主壓縮機中壓縮之前的該氣體排放流，以產生該經壓縮之再循環排放氣；及CO2分離器，而，該分離器與該經壓縮之再循環排放氣經由洗滌流以流體連結，且經配置以排放主要由在氣體膨脹器中膨脹之富含氮氣的氣體所組成之殘餘流，及產生氮排放氣，其中將該氮排放氣注入該第一塔中，以蒸發及冷卻該冷卻水補給流，以排放冷卻之水，且其中將該冷卻之水注入該第二塔中，以冷卻該氣體排放流。
  18. 根據申請專利範圍第17項之系統，其進一步包冷凝器，而該冷凝器與該殘餘流以流體連結，且經配置以降低殘餘流之溫度及從該殘餘流抽取出冷凝之水。
  19. 根據申請專利範圍第17項之系統，其中該蒸發冷卻塔進一步包含幫浦，而該幫浦經配置以加壓冷卻之水，且將該冷卻之水注入該第二塔中，以冷卻該經加壓之再循環氣。
  20. 根據申請專利範圍第19項之系統，其中該第二塔為直接接觸冷卻器。
  21. 根據申請專利範圍第20項之系統，其中該第二塔為多階段直接接觸冷卻器。
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