201250177 六、發明說明： 【發明所屬之技術領域】 本發明係關於碾磨用於氧·燃料燃燒器之燃料的方法及 系統。本發明亦係關於包括此系統之氧-燃料燃燒發電 廠。 【先前技術】 大部分在當今世界使用的能量係源自含碳及氫燃料（諸 如煤、油及天然氣以及其他有機燃料）之燃燒。此燃料生 成含高含量二氧化碳之煙道氣。由於考慮到全球暖化，減 少排放二氧化碳至大氣中之需求日益增加，已開發出方法 來先自煙道氣中移除二氧化碳，然後再將該氣體釋放至大 氣中。 為減少該煙道氣的量，並因此減小發電廠及其氣體清潔 f己置之尺寸，以及為促進純化及移除二氧化碳，可在燃燒 爐中使用氧氣代替空氣（所謂的氧·燃料燃燒），生成具有高 二氧化碳濃度及低氮氣濃度之煙道氣。該氧氣可由藉由空 氣分離單元（ASU)將空氣分離成氧氣流及氮氣流而獲得。 可將該用於氧-燃料燃燒之燃料（諸如煤）先碾磨成粉末， 然後再進入該爐以改善燃燒。 JP 59-024115 A2揭示藉由氧氣滲透膜將空氣分離成富氮 空氣及富氧空氣，之後將煤於該富氮空氣中粉碎並將該粉 碎的煤用富氧空氣燃燒。 【發明内容】 依據本發明之一態樣，提供碾磨用於氧_燃料燃燒器之 162191.doc 201250177 燃料的方法，該方法包括：將空氣分離成具有至少15〇它 之溫度及至少98莫耳。/。氮氣之純度的熱氮氣流，及氧氣 流’將該氮氣流之至少一部分引入至燃料碟磨機；在藉由 該氮氣流形成的富氮氛圍中，利用該燃料碾磨機碾磨該燃 料；使該氮氣流之該至少一部分離開該經碾磨燃料；將該 氧氣流引入至該氧-燃料燃燒器；將該經碾磨燃料輸送至 該氧-燃料燃燒器；及在藉由該氧氣流形成的富氧氛圍 中’利用該氧-燃料燃燒器燃燒該燃料。 依據本發明之另一態樣，提供一種系統，其包括：空氣 分離單元（ASU) ’其經配置用於將空氣分離成具有至少 150°C之溫度及至少98莫耳％氮氣純度的熱氮氣流，及氧 氣流；燃料碾磨機’其經配置用於在藉由該氮氣流形成的 备氮氣圍中犧磨燃料；及氧-燃料燃燒器，其經配置用於 在藉由該氧氣流形成的富氧氛圍中燃燒該經碾磨燃料。 依據本發明之另一態樣’提供包括以上態樣之系統的 氧-燃料燃燒發電廠。 關於本發明之各別態樣之任一項的以上及以下討論在適 用部分亦係關於任何其他態樣。 藉由獲得具有高溫之熱氮氣流並將其引入至該燃料碾磨 機’可在該熱氮氣流之氛圍下碾磨該燃料。因此，該熱氣 流可用於乾燥該燃料’同時亦提供在碾磨/粉碎該燃料期 間降低粉塵爆炸風險的惰性環境。可能期望先乾燥該燃 料，然後再將其燃燒以增加該燃燒器之能效並減少會污染 且增加煙道氣之體積的水蒸氣量。在到達該碾磨機之前， 162191.doc 201250177 該氮氣流可能已膨脹及其溫度可能已降低，但可能仍足夠高 以至少部分乾燥該碾磨機中的燃料。藉由由該具有足夠高 溫度的ASU獲得氮氣流，在該氣流可用於乾燥該燃料之前， 可能不必要藉由該ASU外部的額外熱交換器加熱該氮氣流。 為減少該煙道氣中的氮氣量’將至少大部分該氮氣流在 該燃料到達該燃燒器之前自該燃料中移除，從而減少該煙 道氣體積。 【實施方式】 當前較佳的實施例將參照圖式論述於下文。 本發明之系統及發電廠包括連接其等不同部分並經配置 以使得各別流體及固體材料可視需要流過或被輸送通過該 系統/發電廢的管件。該管件可包括適於控制各別流體及 固體之流動/輸送及性質的導管、閥門、泵、輸送器 '壓 縮機、風扇、膨脹機、喷嘴、熱交換器等。 該熱氮氣流具有至少loot之溫度，諸如至少15〇〇C，至 少200°C，至少22〇t或至少240°C，例如在200。(：及300°C 之間，在220。(：及280。(：之間或在240°C及260°C之間，或約 250 C °此高溫可在自該空氣分離該氮氣流及該氮氣流進 入該燃料碾磨機之間獲得，諸如當在該ASU内與壓縮空氣 熱父換後離開該ASU時，但是該溫度可能不會在通向該燃 料碾磨機的一路上一直如此高。該熱氮氣流可能在到達該 燃料碾磨機之前，例如，在用於能量回收之渦輪機中，藉 由膨脹而稍微冷卻。該氮氣流可便利地在到達該燃料碾磨 機時仍具有高溫，以致其可用於在該碾磨機内乾燥該燃 162191.doc 201250177 料。因此，該氮氣流當進入該燃料碾磨機時，可能具有至 少loot，至少120。(：或至少140〇c之溫度，例如，在1〇代 及20(TC之間，在120〇c&18(rc之間或在14〇<^及i6〇ec之 間，或約15〇°C。 該熱氮氣流具有至少95莫耳％氮氣之高純度，諸如至少 98莫耳％ ’至少99莫耳％或至少99 5莫耳此氮氣流之高 純度增加其惰性並降低在碾磨、乾燥及/或在碾磨之前或 之後的燃料輪送期間該燃料之點火或粉塵爆炸或其類似之 風險。 為改善4氧-燃料燃燒器之能效並減小煙道氣體積，該 氧氣流亦可方便地具有高純度。因此，該氧氣流可具有至 90莫耳。/。氧氣之尚純度，諸如至少％莫耳％，至少μ莫 耳。/〇,至少99莫耳％或至少99.5莫耳〇/〇。 將空氣分離成熱氮氣流及氧氣流可以任何適宜之方式進 行，諸如藉由包括低溫蒸餾空氣。低溫蒸餾對於所揭示的 方法可能係便利的，原因在於可能獲得具極高純度之氮氣 及氧氣流，諸如分別至少95莫耳％、至少98莫耳％或至少 99莫耳％之氮氣及氧氣。 將空氣分離成熱氮氣流及氧氣流可包括在分離之前壓缩 二氣。忒壓縮可便利地為至少部分絕熱以獲得高溫之壓縮 空氣，諸如至少i5〇°c，至少18(rc，至少20〇t，至少 25〇°C或至少300°c，例如在25(rc及35(rc之間，在280〇c 及32〇t之間或約30(TC。接著可使用該熱壓縮空氣藉由熱 父換獲得該熱氮氣流之南溫。因此，該壓縮空氣可在分離 16219l.doc 201250177 之刖冷部，且可加熱該分離的氮氣流。壓縮可以單一的壓 縮步驟進行，或藉由多級壓縮進行。 典型上，使用帶有間歇冷卻的多級壓縮以在ASU中壓縮 該空氣。在大多數情況下，接著利用冷卻水移除該熱量。 接著該移除的熱量可在約4Gt下離開該電廠並將終止於冷 邠塔、空乳冷钾器等中。在該情況下，該熱量將損失，因 未被進步利用在該系統或發電廠中。中間冷卻壓縮之 -優點係所需的軸功率更低。因*匕’令人驚奇的是藉由使 用絕熱壓縮可獲得更低的總能量消耗，而容許將該氮氣流 加熱至使其可以更少或無需另外加熱該氮氣流用於乾燥該 燃料及更少或無需另外乾燥該燃料的溫度。此外，可將該 銷爐中燃料燃燒所需的氧氣預熱。此預熱減少所需的加熱 介質，諸如來自燃料燃燒的熱煙道氣、來自水_蒸汽-循環 的热Λ、或來自水-蒸汽_循環的熱鍋爐給水。因此可減少 總能f消耗（燃料消耗ρ另外，使用絕熱空氣壓縮及廢熱 利用可節約冷卻水。在燃燒硬煤或次煙煤之情況下，燃料 水分之減少容許減小所有煙道氣管道之尺寸並亦可減少冷 凝及移除該煙道氣之水蒸氣所需 的冷卻水量。 因此，改善氧-發電廠之總體熱平衡及水平衡。 應注意，中間冷卻壓縮或絕熱及中間冷卻壓縮之組合亦 °、「與本發明之方法及系統一起使用，只要可獲得足夠高溫 度的氮氣流即可》可配置該壓縮，使得該系統或發電廠之 總能量消耗減少或最小化。 可將全部或僅一部分之由該ASU產出的氮氣流引入至該 16219 丨.doc 201250177 燃料礦磨機。右僅引入一部分至該艰磨機，則可將第一部 分引入至另外的燃料乾燥器，補充在該燃料艰磨機中進行 的乾燥。在燃燒具有高水分含量的燃料（例如，褐煤）的情 況下’使用另外的乾燥器可能尤其便利。用於乾燥具高水 分含量燃料（諸如褐煤）之裝置及方法係為習知發電廠所熟 知。因此，可藉由依據本發明整合該乾燥器及該Asu(廢） 熱而減小此等習用乾燥器之熱需求及其等之尺寸。可配置 該另外的乾燥器以在碾磨該燃料之前或之後將其乾燥但 在碾磨之後另外乾燥該燃料可能係有利的，原因在於經碾 磨燃料可能比未經碾磨燃料具有更大的與該熱氮氣流之接 觸表面，而有利於乾燥。因此，本發明之方法亦可包括： 將該熱氮氣流之第二部分引入至燃料乾燥器；在碾磨該燃 料之前或之後，藉由該燃料乾燥器乾燥該燃料；及將該熱 IL氣流之該第二部分引導離開該經乾燥燃料。類似地，若 需要可連續地使用一或多個另外的乾燥器，使用部分該氮 氣流或其他乾燥介質來乾燥該燃料。 該燃料礙磨機及/或任何另外的乾燥器之富氮氛圍係藉 由該富氮氣流形成、然而]亥富氮氣流可能不僅由該氮氣 流形成。可能可便利地自該燃燒器之下游再循環煙道氣至 該碾磨機以助於為該碾磨機形成適宜的惰性及乾燥氛圍。 藉由結合錢氣流與再循環㈣錢以形成制磨機及/ 或另外的乾燥器之氛圍’可另外使用來自該燃燒器及燃料 燃燒的熱量於乾燥該嫩制· Β -Γ * 价4燃^且可能需要更少的該熱氮氣流。 類似地，在該揪煻#结a .，.、現益處之该虽氧氮圍不僅可由該來自 162191.doc 201250177 ASU的氧乳流形成，並 ^ ^ 〔 由再循％的煙道氣形成。 T此與風扇、壓縮機、 .,機（啫如渦輪機）及/或其他便 利的早兀σ作的任何適宜 ^ ACTT2, s (4如導管）可用於將該氮氣 /瓜自以17引至该燃料儀磨機 ,,^ ^ 俄將该氮氣流引導離開該燃 料’例如’離開該妙·料诚癍 ^ ‘、磨機或離開將燃料自該碾磨機向 该燃k态輸达的輸送器’ ,入 于茨軋軋流自該ASU引至該燃 燒器。除該艰磨機之外，甚佶田姑总友 , 右使用該氮軋流之第二部分於在 另外的乾燥器中乾烨兮.^ ^ ⑽錢枓，則亦可使用此適宜之管道於 將該氮氣流之第二部分自兮 自孩ASU引至該燃料乾燥器並用於 將該氮氣流之第二部分引墓離 〇 d_ 刀5丨導離開該燃料，例如離開該燃料 乾燥器或離開將燃料自該乾择 茨靶琮态向該燃燒器輸送的輸送 器。 可使用任何適宜之輪送器（諸如輸送帶）來傳輸或輸送該 未k礙磨燃料至該燃料礙磨機及/或將經礙磨燃料自該燃 料礙磨機輸送至該燃燒器，可能經由-或數個另外的燃料 乾燥器 因此’本發明之系統亦可包括：經配置用於將該氮氣流 之至少一部分引至該燃料碾磨機的第一管道；經配置用於 將該氮氣流之至少—部分引導離開該經礙磨燃料的第二管 过，、’玉配置用於將該氧氣流引至該氧-燃料燃燒器的第三 管道；及經配置用於將該經碾磨燃料輸送至該氧_燃料燃 燒器的輸送器。 該碾磨機可為用於碾磨/粉碎該燃料並容許氮氣流通過 的任何適宜燃料碾磨機。 16219l.doc 201250177 該另外的乾燥器（若使用）可為用於乾燥該燃料並容許氮 氣流通過的任何適宜燃料乾燥器。 該燃燒器可為任何適宜之氧-燃料燃燒器。 為避免燃料粒子（例如，經碾磨的燃料粉末粒子）在藉由 該氮氣流碾磨及乾燥該燃料期間隨著該氮氣流離開該燃料 罐，該經配置以引導該氮氣流離開該燃料的管道可配置有 (或另外合併）粒子移除器，諸如靜電集塵器、旋風器、過 慮器及/或；條氟器。若使用一另外的乾燥器，則粒子移除 器可與經配置以引導該氮氣流離開該經另外乾燥燃料的管 道合併。或者，可將單一的粒子移除器用於來自該碾磨機 的氮氣流及來自該另外乾燥器的氮氣流二者。 參照圖1 ’現將描述包括依據本發明之系統的特定發電 廠1。 該發電廠1及該系統包括經配置用於艰磨/粉碎該發電廠 燃料（諸如煤）的燃料碾磨機2。該碾磨機2係經由管道或輸 送器連接用於使待碟磨的燃料進入該礙磨機2。該碾磨機2 亦經由管道3連接至該空氣分離單元（ASU)4用於容許氮氣 流自該ASU 4經由該碾磨機2之進氣口進入該礙磨機2。此 外’配置該碾磨機2以經由管道及該碾磨機2之進氣口接收 再循環的煙道氣，該煙道氣係藉由風扇、壓縮機或渦輪機 5再循環。配置管道6以連接該碾磨機2及呈靜電集塵器 (ESP)7之形式的粒子移除器，以使得該氮氣流及/或該再循 環的煙道氣可經由該碾磨機2之出氣口離開該碾磨機2並經 由該ESP 7之進氣口進入該ESP 7。該ESP 7係經配置以移 I62191.doc •12· 201250177 u並返回m隨該it氣流的任何燃料粒？。呈輸送帶8之形 式的輸送益連接该艰磨機2與氧_燃料燃燒器9，使得經碼 磨燃料可藉由該輸送器8自該艰磨機2輸送至該燃燒器9。 配置4儀磨機2之進氣口及出氣口，使得該氮氣及煙道氣 . m橫向於藉由該輸送器8輸送該燃料之方向通過該儀 . 磨機2，因此減少到達該燃燒器9的煙道氣及尤其是氮氣的 !。因此，該碾磨機2可在惰性氮氣及煙道氣氛圍中碾磨 該燃料，減少該礙磨機2中點火或爆炸的風險，同時該熱 氣流亦乾燥該燃料。 亦可使用另-燃料乾燥器1G。該乾燥器職似地經由管 道11連接至該ASU 4並經由管道12連接至該Esp 7，使得熱 氣氣流可經由進1口進入該乾燥㈣’豸過該由輸送器8 知送的經碾磨燃料，同時在垂直於該燃料之輸送方向的方 向上乾燥該燃料，且經由出氣口及該管道12流出該乾燥器 10流向該ESP 7。 除δ亥乾燥器1 〇之外或替代該乾燥器丨〇，可使用利用非該 熱氮氣流之乾燥介質的燃料乾燥器13來乾燥該燃料。 该碾磨機2及該輸送器8及乾燥器10及13可在稍高於環境 之壓力下操作，以避免空氣（及因此氮氣）洩漏進去，其會 - 減小利用氧-燃料燃燒之優勢。 该氧-燃料燃燒器9係配置在該鍋爐14中或與該鍋爐14一 起，並經配置以經由該輸送器8接收該經乾燥及碾磨的燃 料。该燃燒器9係經配置以在藉由來自該ASU 4之富氧氣流 所提供的富氧氛圍中燃燒該燃料，該富氧氣流係經配置以 16219 丨.doc •13· 201250177 經由連接該鍋爐14與該ASU 4的管道並經由該鍋爐14之進 氣口進入該鍋爐14，可能連同藉由風扇、壓縮機或渦輪機 1 5回收的煙道氣。藉由容許該燃燒器9以氧氣替代空氣來 操作’因惰性氮氣已在先前移除，故煙道氣之量減少。該 燃燒可藉由回收煙道氣與使用氧氣之比率來控制。萬—該 ASU失效或若氧氣因其他原因不能被提供至該燃燒器$， 則仍可利用空氣燃燒來確保該廠1的可靠性。 該鋼爐14係經配置以自由該燃燒器9產生的熱量來產生 热汽’該蒸汽被用於藉由渦輪機（未顯示）來發電。 該ASU 4係如上述經由氣體管道連接至該碾磨機2、該乾 燥器1 0及該鍋爐14，使得由該ASU 4產生的熱氮氣流可藉 由官道3及6通過該碾磨機2並經由管道丨丨及丨]通過該乾燥 器〗〇，及由該ASU產出的氧氣流可進入該鍋爐丨4以用於在 該燃燒器9燃燒該燃料《若需要，來自該ASu的熱氮氣流 可在分別進入該碾磨機2及該乾燥器10之前藉由熱交換器 1 6另外加熱。在該氣流進入該鍋爐丨4之前可方便地藉由熱 交換器17預熱該氧氣流。 將煙道氣清潔配置連接至該鍋爐14以清潔由氧_燃料燃 燒所產生的煙道氣。因此該煙道氣可在任何排氣被釋放至 大氣之前連續地通過數個不同的清潔單元。在圖1之特定 發電廠中，該煙道氣通過如上述經配置以冷卻離開該鍋爐 14的煙道氣並加熱再循環至該碾磨機2及該鍋爐14的煙道 氣的煙道氣熱交換器、用於自該煙道氣移除粒子的靜電集 塵器19、煙道氣壓縮機20、煙道氣冷卻器21 '濕煙道氣脫 I6219I.doc 14 201250177 疏單元22、煙道氣冷凝器23、及用於自該煙道氣移除二氧 化碳的氣體處理單元24。 參照圖2，現將描述ASU 4之特定實施例。 絕熱壓縮機25係經配置以壓縮周溫及周壓之空氣至在 200°C及300°C之間之溫度，諸如20〇°C及250t，及在2至 20巴之間之壓力，諸如3至6巴，例如約5巴。配置該壓縮 機以使得經由管道進入之空氣可經由進氣口進入該壓縮機 2.5。該壓縮機25係經由氣體管道連接至熱交換器26，以使 得經壓縮空氣可經由該壓縮機25之出氣口及該管道離開該 壓縮機25以經由該熱交換器26之進氣口進入該熱交換器 26 ’而藉由該熱交換器26冷卻。 低溫瘵餾單元27係與該熱交換器26流體連接，使得經冷 卻的壓縮空氣（其可能經至少部分液化）可經由流體管道及 該蒸館單元27之流體進口進入該蒸餾單元27。該蒸餾單元 27可（例如）為在習知低溫ASU中使用的習知蒸餾單元。配 3[該療館單元27以低溫蒸餾該壓縮空氣，使得該空氣被分 喊成具有99.5莫耳％之純度的至少一氮氣流體流（其可為氣 體或液體或其混合物）及至少一氧氣流體流（其可為氣體或 液體或其混合物），及可能為氬氣流體流及/或其他氣體成 分之流。另外，該蒸餾單元27係與該熱交換器26流體連 接，以使知s玄氮氣及氧氣流體流可經由各自的流體出口離 開該瘵餾單元27並經由各自的管道及該熱交換器26之流體 進口傳遞至該熱交換器26中。 配置呈渦輪機28之形式的膨脹機，以使該至少一氮氣流 16219l.doc -15. 201250177 及可能亦使其他分離產物膨脹，同時自該膨脹回收能量。 該渦輪機28係經由分別用於該氮氣流及視情況該氧氣流的 管道來與該熱交換器26流體連接，以使得該氮氣及氧氣流 可經由s亥熱交換器26的各自出氣口離開該熱交換器26，經 由各自的導管自該熱交換器26傳遞至該渦輪機28並經由各 自的進氣口進入該渦輪機28。典型上，該膨脹機28包括分 別用於該氮氣及氧氣流的個別渦輪機。可配置該膨脹機2 8 用於多級膨脹。該膨脹機28係經配置以使該熱氮氣流自約 250 C之溫度及在2至20巴間之壓力（諸如3至6巴，例如約5 巴）膨脹至約150°C之溫度及僅稍高於環境之壓力。在藉由 該膨脹機28膨脹後，如以上參照圖1所討論，該氧氣流可 被引入至該鋼爐14及該氮氣流可被引入至該礙磨機2及可 能地該乾燥器1 0。 如圖2中所顯示，至少一部分來自該蒸餾器以的氮氣流 可另外或替代地繞過該熱交換器26及/或該膨脹機28，例 如可能經由該視情況的圖丨之預熱熱交換器16直接引入至 該碾磨機2及/或該乾燥器10。 亦可方便地在膨脹機（例如，膨脹機28)中使該氧氣流膨 脹，例如以回收能量。其後可將該氧氣流引至該鍋爐14及 該燃燒器9。尤其若該氧氣流已經膨脹，則在進入該鍋爐 14之則可方便地（例如）藉由與蒸汽熱交換來預熱該氧氣 流》如圖2中所顯示，該氧氣流可在該膨脹機“中膨脹或 繞過該膨脹機28，例如直接引至該鍋爐14，或部分該氧氣 流可通過§玄膨脹機28，而另一部分繞過膨脹機28。 162191.doc •16· 201250177 視情況地，可先使用熱交換器29來預熱該氮氣流，及視 :青況s亥氧氣流’然後再藉由該膨服機2 8膨脹β該熱交換器 :!9可（例如）使用來自該鍋爐14的熱煙道氣、來自該發電廠1 之水/蒸汽循環的蒸汽及/或來自該發電廠1之水/蒸汽循環 的鍋爐給水作為加熱介質。 如上述’該熱交換器2 6係與該壓縮機2 5、該蒸儲單元2 7 及5亥膨脹機28流體連接。配置該熱交換器26，以藉由與該 蒸餾產物（即’該氮氣及氧氣流）熱交換來冷卻該壓縮空 氣。可能亦需要除該氮氣及氧氣流之外的另一冷卻介質。 因此可配置該熱交換器26，以將該壓縮空氣自在2〇(rc至 250C之間之溫度及在2至20巴之間之壓力（諸如3至6巴， 例如約5巴）冷卻至在5〇°C至lOOt：之間之溫度及2至20巴之 間之壓力（諸如3至6巴，例如約5巴），將該氮氣流自在〇°c 至30°C之間之溫度（諸如約lot )及2至20巴之間之壓力（諸 如3至6巴’例如約5巴）加熱至在150°C至250。(：之間之溫度 及在2至2 0巴之間之壓力（諸如3至6巴，例如約5巴），及將 該氧氣流自在〇°C至30°C之間之溫度（諸如約1 〇)及在1至2〇 巴之間之壓力（諸如1至3巴，例如約1 · 2巴）加熱至在15 〇。〇 至250°C之間之溫度及在1至3巴之間之壓力（例如約1.2 巴）。 參照圖3 ’現將描述依據本發明之方法的特定實施例 100。 藉由該ASU 4 ’將空氣分離成（步驟101)熱氮氣流及氧氣 流。將s亥熱氦i氣流引至s玄燃料礙磨機2並將該氧氣流引至 162l9l.doc 17 201250177 該氧-燃料燃燒器9。 在該燃料碾磨機2中，在藉由來自該ASU 4之熱氮氣流形 成的富氮氛圍中，碾磨（步驟102)燃料（例如煤）。使該氮氣 流流過該碾磨機2 ’以使得至少大部分該氮氣自該燃料移 除（步驟103)且並不跟隨該燃料至該燃燒器9。 藉由該輸送器8將該經碾磨燃料輸送至該燃燒器9，在此 其在藉由來自該ASU 4之氧氣流所形成的富氧氛圍下進行 氧-燃料燃燒（步驟104)。 雖然本發明已參照若干較佳實施例描述，但熟習此項技 術者應瞭解可在不脫離本發明之範圍内進行多種改變及可 以等效物替代其要素。此外，可在不脫離其實質範圍内進 行許多調整以使特定情況或材料適於本發明之教義。因 此，本發明不欲受限於經揭示作為用於實施本發明之當前 涵蓋的最佳模式的特定實施例，反之本發明將包含所有落 在隨附申请專利範圍之範脅内的實施例。此外，術語第 一、第一等之使用並不指示任何順序或重要性或時序，而 係術語第一、第二等係用來區分一個元素與另一個。 【圖式簡單說明】 圖1係包括依據本發明之系統的發電廠之一實施例的示 意圖。 圖2係可包括在依據本發明之系統中的空氣分離單元之 一實施例的示意圖。 圖3係依據本發明之方法的一實施例的示意流程圖。 【主要元件符號說明】 162191.doc •18- 201250177 1 發電廠 2 燃料碾磨機 3 管道 4 空氣分離單元 5 渦輪機 6 管道 7 靜電集塵器 8 輸送帶 9 燃燒器 10 燃料乾燥器 11 管道 12 管道 13 燃料乾燥器 14 鋼爐 15 滿輪機 16 熱交換器 17 熱交換器 19 靜電集塵器 20 煙道氣壓縮機 21 煙道氣冷卻器 22 濕煙道氣脫硫單元 23 煙道氣冷凝器 24 氣體處理單元 25 絕熱壓縮機 16219l.doc • 19- 201250177 26 熱交換器 27 低溫蒸餾單元 28 涡輪機 29 熱交換器 162191.doc -20*201250177 VI. Description of the Invention: [Technical Field of the Invention] The present invention relates to a method and system for milling a fuel for an oxygen fuel burner. The invention is also directed to an oxy-fuel combustion power plant including such a system. [Prior Art] Most of the energy used in today's world is derived from the combustion of carbon and hydrogen fuels such as coal, oil and natural gas and other organic fuels. This fuel produces flue gas with a high content of carbon dioxide. Due to the increasing global demand for carbon dioxide emissions into the atmosphere, a method has been developed to remove carbon dioxide from the flue gas before releasing it into the atmosphere. In order to reduce the amount of flue gas, and thus reduce the size of the power plant and its gas cleaning, and to promote purification and removal of carbon dioxide, oxygen can be used in the furnace instead of air (so-called oxygen/fuel combustion) ), generating flue gas having a high carbon dioxide concentration and a low nitrogen concentration. This oxygen can be obtained by separating air into an oxygen stream and a nitrogen stream by an air separation unit (ASU). The fuel for oxy-fuel combustion, such as coal, can be milled into a powder and then reintroduced into the furnace to improve combustion. JP 59-024115 A2 discloses the separation of air into nitrogen-enriched air and oxygen-enriched air by means of an oxygen permeable membrane, after which the coal is pulverized in the nitrogen-enriched air and the pulverized coal is burned with oxygen-enriched air. SUMMARY OF THE INVENTION In accordance with one aspect of the present invention, a method of milling 162191.doc 201250177 fuel for an oxy-fuel burner is provided, the method comprising: separating air to have a temperature of at least 15 Torr and at least 98 ear. /. a hot nitrogen stream of nitrogen purity, and an oxygen stream 'introducing at least a portion of the nitrogen stream to a fuel disc mill; the fuel mill is used to grind the fuel in a nitrogen-rich atmosphere formed by the nitrogen stream; Passing at least a portion of the nitrogen stream away from the milled fuel; introducing the oxygen stream to the oxy-fuel burner; delivering the milled fuel to the oxy-fuel burner; and flowing through the oxygen The oxy-fuel burner is used to burn the fuel in the formed oxygen-rich atmosphere. In accordance with another aspect of the present invention, a system is provided comprising: an air separation unit (ASU) configured to separate air into hot nitrogen having a temperature of at least 150 ° C and a nitrogen purity of at least 98 mol % a flow, and a flow of oxygen; a fuel mill 'configured to sacrifice fuel in a nitrogen blanket formed by the flow of nitrogen; and an oxy-fuel burner configured to flow through the oxygen The milled fuel is burned in the formed oxygen-rich atmosphere. According to another aspect of the present invention, an oxy-fuel combustion power plant including the above aspect is provided. The above and below discussion of any of the various aspects of the invention is also in the applicable section with respect to any other aspect. The fuel can be milled under the atmosphere of the hot nitrogen stream by obtaining a hot nitrogen stream having a high temperature and introducing it to the fuel mill. Thus, the hot gas stream can be used to dry the fuel' while also providing an inert environment that reduces the risk of dust explosion during milling/pulverization of the fuel. It may be desirable to first dry the fuel and then burn it to increase the energy efficiency of the burner and reduce the amount of water vapor that would contaminate and increase the volume of the flue gas. Before reaching the mill, 162191.doc 201250177 The nitrogen stream may have expanded and its temperature may have decreased, but may still be high enough to at least partially dry the fuel in the mill. By obtaining a nitrogen stream from the ASU having a sufficiently high temperature, it may not be necessary to heat the nitrogen stream by an additional heat exchanger external to the ASU before the gas stream can be used to dry the fuel. To reduce the amount of nitrogen in the flue gas, at least a majority of the nitrogen stream is removed from the fuel before it reaches the burner, thereby reducing the flue gas volume. [Embodiment] The presently preferred embodiment will be discussed below with reference to the drawings. The system and power plant of the present invention includes tubing that connects different portions thereof and is configured such that individual fluids and solid materials can flow through or be transported through the system/power generation waste as desired. The tubular member may include conduits, valves, pumps, conveyors, compressors, fans, expanders, nozzles, heat exchangers, and the like, adapted to control the flow/delivery and properties of the respective fluids and solids. The hot nitrogen stream has a temperature of at least loot, such as at least 15 ° C, at least 200 ° C, at least 22 ° C or at least 240 ° C, for example at 200. (Between and 300 ° C, at 220 ° (: and 280. (: between or between 240 ° C and 260 ° C, or about 250 ° ° ° high temperature can separate the nitrogen stream from the air and The nitrogen stream is obtained between the fuel mills, such as when leaving the ASU after being replaced with the compressed air in the ASU, but the temperature may not be consistent along the way to the fuel mill. The hot nitrogen stream may be slightly cooled by expansion prior to reaching the fuel mill, for example, in a turbine for energy recovery. The nitrogen stream may conveniently have a flow when it reaches the fuel mill. High temperature so that it can be used to dry the fuel in the mill 162191.doc 201250177. Therefore, the nitrogen stream may have at least a loot of at least 120 when entering the fuel mill. (: or at least 140 〇c The temperature, for example, is between 1 〇 and 20 (TC), between 120 〇c & 18 (rc or between 14 〇 <^ and i6〇ec, or about 15 ° C. The hot nitrogen stream Having a high purity of at least 95 mol% nitrogen, such as at least 98 mol% 'at least 99 mol% or at least 99 5 mo The high purity of this nitrogen stream increases its inertness and reduces the risk of ignition or dust explosion of the fuel during milling, drying and/or fuel transfer before or after milling or the like. To improve 4 oxy-fuel combustion The energy efficiency of the device and the volume of the flue gas are reduced, and the oxygen flow can also conveniently have a high purity. Therefore, the oxygen flow can have a purity of 90 mol% of oxygen, such as at least % mol%, at least μ Mohr / / 〇, at least 99 mol % or at least 99.5 mo 〇 / 〇. Separating air into a stream of hot nitrogen and oxygen can be carried out in any suitable manner, such as by including cryogenically distilled air. The method may be convenient because it is possible to obtain a very high purity nitrogen and oxygen stream, such as at least 95 mol%, at least 98 mol% or at least 99 mol% nitrogen and oxygen, respectively. The nitrogen stream and the oxygen stream may comprise compressing the second gas prior to separation. The helium compression may conveniently be at least partially adiabatic to obtain a high temperature compressed air, such as at least i5 〇 ° C, at least 18 (rc, at least 20 〇 t At least 25 ° C or at least 300 ° C, for example between 25 (rc and 35 (rc, between 280 ° c and 32 ° t or about 30 (TC). The hot compressed air can then be used by the hot parent The south temperature of the hot nitrogen stream is obtained. Therefore, the compressed air can be separated from the cold portion of 16219l.doc 201250177, and the separated nitrogen stream can be heated. The compression can be performed in a single compression step, or by multi-stage compression. Typically, multi-stage compression with intermittent cooling is used to compress the air in the ASU. In most cases, this heat is then removed using cooling water. The removed heat can then exit at about 4 Gt. The power plant will be terminated in a cold tower, an empty milk pot, etc. In this case, the heat will be lost as it is not being utilized in the system or power plant. Intercooling compression - the advantage is that the required shaft power is lower. It is surprising that the lower total energy consumption can be obtained by using adiabatic compression, while allowing the nitrogen stream to be heated to a lower or no additional heating of the nitrogen stream for drying the fuel and less. Or there is no need to additionally dry the temperature of the fuel. In addition, the oxygen required to burn the fuel in the pin furnace can be preheated. This preheating reduces the required heating medium, such as hot flue gas from fuel combustion, enthalpy from water-steam-cycle, or hot boiler feed water from water-steam_cycle. Therefore, the total energy consumption can be reduced (fuel consumption ρ. In addition, the use of adiabatic air compression and waste heat utilization can save cooling water. In the case of burning hard coal or sub-bituminous coal, the reduction of fuel moisture allows to reduce the size of all flue gas pipes. It also reduces the amount of cooling water required to condense and remove the water vapor from the flue gas. Therefore, improve the overall heat balance and water balance of the oxygen-power plant. It should be noted that the combination of intercooling compression or adiabatic and intercooling compression is also °, "Use with the method and system of the present invention, as long as a nitrogen stream of sufficiently high temperature is available" can be configured to reduce or minimize the total energy consumption of the system or power plant. A portion of the nitrogen stream produced by the ASU is introduced to the 16219 丨.doc 201250177 fuel miner. The right part is only introduced to the hard mill, and the first portion can be introduced to the additional fuel dryer to supplement the fuel. Drying in a tough mill. In the case of burning fuels with a high moisture content (for example, lignite), the use of additional dryers may be Convenience. Apparatuses and methods for drying high moisture content fuels, such as lignite, are well known in the art. Thus, this can be reduced by integrating the dryer and the Asu heat in accordance with the present invention. The heat demand of the conventional dryer and its dimensions may be configured. It may be advantageous to configure the additional dryer to dry it before or after milling the fuel but to otherwise dry the fuel after milling. The milled fuel may have a greater contact surface with the unheated fuel stream than the hot nitrogen stream to facilitate drying. Thus, the method of the present invention may also include: introducing the second portion of the hot nitrogen stream to the fuel drying The fuel is dried by the fuel dryer before or after milling the fuel; and the second portion of the hot IL gas stream is directed away from the dried fuel. Similarly, one or more may be used continuously if desired a plurality of additional dryers, using a portion of the nitrogen stream or other drying medium to dry the fuel. The nitrogen-rich atmosphere of the fuel barrier and/or any additional dryer is by the nitrogen-rich atmosphere The flow formation, however, may be formed not only by the nitrogen stream. It may be convenient to recycle the flue gas from the downstream of the burner to the mill to help create a suitable inertness for the mill and Dry atmosphere. By combining the money flow and recycling (4) money to form the atmosphere of the mill and / or another dryer 'can additionally use the heat from the burner and fuel to dry the tender · Β -Γ * The price is 4 and may require less of this hot nitrogen stream. Similarly, in the 揪煻# junction a.,., the current benefit of the oxygen-nitrogen can be not only from the oxy-emulsion from 162191.doc 201250177 ASU Formed, and ^ ^ [formed by the re-circulation of % of flue gas. T This is suitable for fans, compressors, ., machines (such as turbines) and / or other convenient early 兀 AC ACTT2, s ( 4, such as a conduit) can be used to direct the nitrogen/melon to the fuel mill, and the nitrogen flow is directed away from the fuel 'for example, 'to leave the wonderful material ^ 癍 ^ ', mill or Leaving the conveyor that delivers fuel from the mill to the combustion state, into the rolling stream The ASU introduced to the burner. In addition to the hard grinding machine, Mr. Tian Gu, the second part of the nitrogen rolling stream is used to dry in another dryer. ^ ^ (10) Qian Wei, you can also use this suitable pipeline The second portion of the nitrogen stream is directed from the child ASU to the fuel dryer and used to direct the second portion of the nitrogen stream from the 〇d_ knife 5 to exit the fuel, such as leaving the fuel dryer or Leaving a conveyor that delivers fuel from the dry target to the burner. Any suitable wheeler, such as a conveyor belt, may be used to transport or transport the unimpeded fuel to the fuel obstruction machine and/or to transport the obstructed fuel from the fuel obstruction machine to the combustor, possibly The system of the present invention may also include: a first conduit configured to direct at least a portion of the nitrogen stream to the fuel mill; configured to vaporize the nitrogen gas via - or a plurality of additional fuel dryers At least a portion of the flow exits the second tube that is obstructed by the fuel, < jade is configured to direct the flow of oxygen to the third conduit of the oxy-fuel burner; and configured to mill the The milled fuel is delivered to the conveyor of the oxy-fuel burner. The mill can be any suitable fuel mill for milling/pulverizing the fuel and allowing the flow of nitrogen. 16219l.doc 201250177 The additional dryer, if used, can be any suitable fuel dryer for drying the fuel and allowing the flow of nitrogen gas. The burner can be any suitable oxy-fuel burner. To prevent fuel particles (eg, milled fuel powder particles) from exiting the fuel tank as it flows away from the fuel tank during milling and drying of the fuel by the flow of nitrogen, the configuration is configured to direct the flow of nitrogen away from the fuel. The conduits may be configured with (or otherwise combined with) particle removers, such as electrostatic precipitators, cyclones, filters, and/or strips. If an additional dryer is used, the particle remover can be combined with a conduit configured to direct the flow of nitrogen away from the otherwise dried fuel. Alternatively, a single particle remover can be used for both the nitrogen stream from the mill and the nitrogen stream from the additional dryer. Referring to Figure 1 ', a specific power plant 1 including a system in accordance with the present invention will now be described. The power plant 1 and the system include a fuel mill 2 configured to rigor/grind the power plant fuel, such as coal. The mill 2 is connected via a pipe or a conveyor for bringing the fuel to be ground into the obstruction machine 2. The mill 2 is also connected via a line 3 to the air separation unit (ASU) 4 for allowing nitrogen flow from the ASU 4 to enter the obstruction machine 2 via the inlet of the mill 2. Further, the mill 2 is configured to receive recirculated flue gas via a conduit and an inlet of the mill 2, the flue gas being recirculated by a fan, compressor or turbine 5. A conduit 6 is provided to connect the mill 2 and a particle remover in the form of an electrostatic precipitator (ESP) 7 such that the nitrogen stream and/or the recycled flue gas can pass through the mill 2 The air outlet exits the mill 2 and enters the ESP 7 via the air inlet of the ESP 7. The ESP 7 is configured to move I62191.doc •12· 201250177 u and return m any fuel particles with the it airflow? . The conveyor in the form of a conveyor belt 8 connects the impeller 2 and the oxy-fuel burner 9 so that the coded fuel can be delivered from the rig 2 to the burner 9 by means of the conveyor 8. Configuring the inlet and outlet of the instrument mill 2 such that the nitrogen and flue gas. m is transverse to the direction in which the fuel is delivered by the conveyor 8 through the mill. The mill 2, thus reducing the arrival of the burner 9 flue gas and especially nitrogen! Therefore, the mill 2 can grind the fuel in an inert nitrogen and flue gas atmosphere, reducing the risk of ignition or explosion in the obstruction machine 2, while the hot gas stream also dries the fuel. An alternative fuel dryer 1G can also be used. The dryer is connected to the ASU 4 via a conduit 11 and to the Esp 7 via a conduit 12 such that a stream of hot gas can enter the dryer via a port (four) 'passing through the milled by the conveyor 8 The fuel is simultaneously dried in a direction perpendicular to the direction of transport of the fuel, and flows out of the dryer 10 through the gas outlet and the conduit 12 to the ESP 7. In addition to or in lieu of the dryer, a fuel dryer 13 that utilizes a drying medium other than the hot nitrogen stream may be used to dry the fuel. The mill 2 and the conveyor 8 and dryers 10 and 13 can be operated at slightly above ambient pressure to prevent air (and therefore nitrogen) from leaking in, which would - reduce the advantages of utilizing oxy-fuel combustion . The oxy-fuel burner 9 is disposed in or associated with the boiler 14 and is configured to receive the dried and milled fuel via the conveyor 8. The combustor 9 is configured to combust the fuel in an oxygen-rich atmosphere provided by an oxygen-rich stream from the ASU 4, the oxygen-rich stream being configured to connect the boiler to 16219 doc.doc •13·201250177 14 enters the boiler 14 with the conduit of the ASU 4 and through the inlet of the boiler 14, possibly together with flue gas recovered by a fan, compressor or turbine 15. By allowing the burner 9 to operate with oxygen instead of air, the amount of flue gas is reduced because the inert nitrogen has been previously removed. This combustion can be controlled by the ratio of the recovered flue gas to the oxygen used. If the ASU fails or if oxygen cannot be supplied to the burner for other reasons, air combustion can still be utilized to ensure the reliability of the plant 1. The steel furnace 14 is configured to free heat generated by the burner 9 to generate hot steam. The steam is used to generate electricity by a turbine (not shown). The ASU 4 is connected to the mill 2, the dryer 10 and the boiler 14 via a gas line as described above, so that the hot nitrogen stream generated by the ASU 4 can pass through the mill through the official passages 3 and 6. 2 and through the pipe 丨 and 丨] through the dryer 〇, and the oxygen stream produced by the ASU can enter the boiler 丨 4 for burning the fuel at the burner 9 "If necessary, from the ASu The hot nitrogen stream can be additionally heated by heat exchanger 16 before entering the mill 2 and the dryer 10, respectively. The oxygen stream can be conveniently preheated by heat exchanger 17 before the gas stream enters the boiler crucible 4. A flue gas cleaning configuration is coupled to the boiler 14 to clean the flue gas produced by the oxy-fuel combustion. Thus the flue gas can be continuously passed through several different cleaning units before any exhaust gas is released to the atmosphere. In the particular power plant of FIG. 1, the flue gas is configured to cool the flue gas exiting the boiler 14 as described above and to heat the flue gas recirculated to the mill 2 and the flue gas of the boiler 14. Heat exchanger, electrostatic precipitator 19 for removing particles from the flue gas, flue gas compressor 20, flue gas cooler 21 'wet flue gas de-I6219I.doc 14 201250177 spalling unit 22, smoke A gas condenser 23, and a gas processing unit 24 for removing carbon dioxide from the flue gas. Referring to Figure 2, a particular embodiment of ASU 4 will now be described. The adiabatic compressor 25 is configured to compress ambient and ambient air to a temperature between 200 ° C and 300 ° C, such as 20 ° C and 250 t, and a pressure between 2 and 20 bar, such as 3 to 6 bar, for example about 5 bar. The compressor is configured such that air entering via the conduit can enter the compressor 2.5 via the air inlet. The compressor 25 is connected to the heat exchanger 26 via a gas conduit such that compressed air can exit the compressor 25 via the gas outlet of the compressor 25 and the conduit to enter the inlet via the heat exchanger 26 The heat exchanger 26' is cooled by the heat exchanger 26. The cryogenic rectification unit 27 is fluidly coupled to the heat exchanger 26 such that the cooled compressed air (which may be at least partially liquefied) can enter the distillation unit 27 via the fluid conduit and the fluid inlet of the vaporizer unit 27. The distillation unit 27 can, for example, be a conventional distillation unit used in conventional low temperature ASUs. 3 [The treatment unit 27 distills the compressed air at a low temperature such that the air is shouted into at least one nitrogen fluid stream (which may be a gas or a liquid or a mixture thereof) having a purity of 99.5 mol% and at least one oxygen The fluid stream (which may be a gas or a liquid or a mixture thereof), and possibly a stream of argon fluid and/or other gas components. In addition, the distillation unit 27 is fluidly coupled to the heat exchanger 26 such that the squid nitrogen and oxygen fluid streams can exit the retort unit 27 via respective fluid outlets and via respective conduits and the heat exchanger 26 The fluid inlet is delivered to the heat exchanger 26. An expander in the form of a turbine 28 is configured to expand the at least one nitrogen stream 16219l.doc -15. 201250177 and possibly also other separated products while recovering energy from the expansion. The turbine 28 is fluidly coupled to the heat exchanger 26 via conduits for the nitrogen stream and optionally the oxygen stream, such that the nitrogen and oxygen streams exit the respective outlets of the heat exchanger 26 Heat exchangers 26 are transferred from the heat exchanger 26 to the turbine 28 via respective conduits and into the turbine 28 via respective intake ports. Typically, the expander 28 includes individual turbines for the flow of nitrogen and oxygen, respectively. The expander 28 can be configured for multi-stage expansion. The expander 28 is configured to expand the hot nitrogen stream from a temperature of about 250 C and a pressure between 2 and 20 bar (such as 3 to 6 bar, such as about 5 bar) to a temperature of about 150 ° C and only Slightly above the pressure of the environment. After expansion by the expander 28, as discussed above with reference to Figure 1, the oxygen stream can be introduced to the steel furnace 14 and the nitrogen stream can be introduced to the sander 2 and possibly the dryer 10 . As shown in Figure 2, at least a portion of the nitrogen stream from the distiller may additionally or alternatively bypass the heat exchanger 26 and/or the expander 28, such as may be preheated via the conditional map. The exchanger 16 is introduced directly to the mill 2 and/or the dryer 10. It is also convenient to expand the oxygen stream in an expander (e.g., expander 28), for example to recover energy. This oxygen stream can then be directed to the boiler 14 and the burner 9. In particular, if the oxygen stream has expanded, then entering the boiler 14 may conveniently preheat the oxygen stream, for example by heat exchange with steam, as shown in Figure 2, which may be in the expander. "Medium expands or bypasses the expander 28, for example, directly to the boiler 14, or a portion of the oxygen stream can pass through the sigma expander 28 while the other portion bypasses the expander 28. 162191.doc •16· 201250177 Depending on the situation The heat exchanger 29 can be used to preheat the nitrogen stream, and the oxygen flow can be expanded by the expansion machine. The heat exchanger can be used, for example, by using the expansion machine. The hot flue gas from the boiler 14, the steam from the water/steam cycle of the power plant 1, and/or the boiler feed water from the water/steam cycle of the power plant 1 as a heating medium. The 6 series is in fluid connection with the compressor 25, the steam storage unit 2 7 and the 5 expander 28. The heat exchanger 26 is arranged to exchange heat with the distillation product (ie, the nitrogen and oxygen streams). Cooling the compressed air. It may also require another addition to the nitrogen and oxygen streams. Cooling medium. The heat exchanger 26 can therefore be configured to self-contain the compressed air at a temperature between 2 rc and 250 C and at a pressure between 2 and 20 bar (such as 3 to 6 bar, for example about 5 bar). Cooling to a temperature between 5 ° C and 100 t: and a pressure between 2 and 20 bar (such as 3 to 6 bar, for example about 5 bar), the nitrogen flow is between 〇 ° c and 30 ° C The temperature (such as about lot) and the pressure between 2 and 20 bar (such as 3 to 6 bar 'e.g., about 5 bar) are heated to between 150 ° C and 250. (: between the temperature and between 2 and 20 bar The pressure between (such as 3 to 6 bar, for example about 5 bar), and the flow of oxygen from 〇 ° C to 30 ° C (such as about 1 〇) and between 1 and 2 〇 The pressure (such as 1 to 3 bar, for example about 1.25 bar) is heated to a temperature between 15 〇 and 250 to 250 ° C and a pressure between 1 and 3 bar (for example about 1.2 bar). A specific embodiment 100 of the method according to the invention will now be described. The air is separated (step 101) by a hot nitrogen stream and a stream of oxygen by the ASU 4'. The gas stream is directed to the s Machine 2 and the oxygen Lead to 162l9l.doc 17 201250177 The oxy-fuel burner 9. In the fuel mill 2, the fuel is milled (step 102) in a nitrogen-rich atmosphere formed by a stream of hot nitrogen from the ASU 4 ( For example, coal). The nitrogen stream is passed through the mill 2' such that at least a majority of the nitrogen is removed from the fuel (step 103) and the fuel is not followed to the burner 9. By the conveyor 8 The milled fuel is delivered to the combustor 9 where it is subjected to oxy-fuel combustion under an oxygen-rich atmosphere formed by the oxygen stream from the ASU 4 (step 104). While the invention has been described with respect to the preferred embodiments of the present invention, it will be understood by those skilled in the art In addition, many modifications may be made to adapt a particular situation or material to the teachings of the invention. Therefore, the present invention is not intended to be limited to the specific embodiments disclosed as the best mode of the present invention. In addition, the use of the terms first, first, etc. does not denote any order or importance or timing, and the terms first, second, etc. are used to distinguish one element from another. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic illustration of one embodiment of a power plant including a system in accordance with the present invention. Figure 2 is a schematic illustration of one embodiment of an air separation unit that may be included in a system in accordance with the present invention. 3 is a schematic flow diagram of an embodiment of a method in accordance with the present invention. [Explanation of main component symbols] 162191.doc •18- 201250177 1 Power plant 2 Fuel mill 3 Pipe 4 Air separation unit 5 Turbine 6 Pipe 7 Electrostatic dust collector 8 Conveyor belt 9 Burner 10 Fuel dryer 11 Pipe 12 Pipe 13 Fuel dryers14 Steel furnaces15 Full turbines16 Heat exchangers17 Heat exchangers19 Electrostatic dust collectors20 Flue gas compressors21 Flue gas coolers22 Wet flue gas desulfurization units 23 Flue gas condensers24 Gas treatment unit 25 adiabatic compressor 16219l.doc • 19- 201250177 26 heat exchanger 27 cryogenic distillation unit 28 turbine 29 heat exchanger 162191.doc -20*