201245639 六、發明說明： 【發明所屬之技術領域】 本發明大致上係關於自煙道氣減除氮氧化物。特定言 之’本發明係關於一種用於低Ν〇χ排放之乾燥劑再生系 統。本發明進一步係關於一種具有低]^〇?^排放之乾燥劑再 生之方法。 【先前技術】 在諸如發電廠之燃燒廠中，於諸如媒、油、泥炭、廢棄 物等之燃料燃燒期間，產生熱製程氣體，此製程氣體尤其 包含二氧化碳C〇2。隨著漸增的環境需求，已開發出多種 裝程來自製程狀體移除二氧化碳。此種製程之一實例為所 謂的氧-燃料製程。在氧-燃料製程中，使諸如上述燃料中 之一者之燃料在貧氮氣體之存在下燃燒。在氧·燃料燃燒 製程中產生富二氧化碳煙道氣，可將其處置以減少二氧化 碳之排放量。該富二氧化碳煙道氣亦可包含污染性氣體， 例如NOx氣體。亦應移除該等污染物。有多種不同方法可 用於自氣體流移除氮氧化物，例如，可藉由使用Gpu廢氣 或藉由使用所謂的DeN〇x單元，#用催化還原作用移除該 等NOx氣體。 US 6 146 605論述用於減少煙道氣之方法，例 如，選擇性催化還原（SCR)及選擇性非催化還原仰叫及 其組合。本文中使用氣_3)作為還原氣體來移除該等 NOx氣體。該系統並未連接至用於再生乾_之系统。 於⑽4 533 365中，利用分子筛分離含N〇x氣體之氣體 162823.doc 201245639 且將其再循環至該系統中。 在以往使用的乾燥劑再生系統中，會共吸附例如Ν〇χ氣 體之污染物。當隨後再生該等乾燥劑時’亦釋放出1^〇^氣 體，此導致再生廢氣中出現不利的^^◦乂濃度峰。 因此需要解決問題，以在乾燥劑再生時避免排放或實質 上避免排放NOx。 【發明内容】 本發明之一目標係提供一種用於純化在於含氧氣體之存 在下燃燒燃料之鍋爐中所產生且受Ν〇χ氣體污染之富二氧 化碳煙道氣之系統。 本發明之-實施例為一種用於純化在於含氧氣體之存在 下燃燒燃料之鍋爐中所產生且受Ν〇χ氣體污染之富二氧化 碳煙道氣之系統，其中該系統包括： 一或多個氣體乾燥器，其含有用於移除該經進一步壓縮 之富二氧化碳煙道氣中之至少一部分水含量之乾燥劑； 用於再生该等乾燥器之乾燥劑之與該等乾燥器連接之閉 環’其中Ν0χ氣體實質上分開地自水蒸氣移除。 根據本發明之系統僅產生低再生廢氣流，此點對環境有 利。此外，ΝΟχ排放量相較已知方法而言亦減少及藉由該 系統亦避免Ν〇χ氣體之峰值排放。 該系統m點為⑶2之_量減少，於根據本發明 之系統中，損耗量少於〇.2體積〇/〇。 本發明之-實施例為-種如上述之㈣純化煙道氣之系 統，其中該閉環包括利用可吸收於再生期間自該乾燥器移 162823.doc 201245639 除之NOx氣體之洗務介質操作之條氣塔。 本發明之一實施例為一種如上述之用於純化富二氧化碳 煙道氣之系統，其中自該乾燥器解吸之水將在洗滌塔中冷 凝。 在根據本發明之用於純化富二氧化碳煙道氣之系統中， 其中該洗滌介質之pH可經適宜調整以最大化該氣體之洗 蘇。 本發明之一實施例為一種用於純化富二氧化碳煙道氣之 系統，其中該pH係藉由添加選自氨(而3)及鹼金屬氫氧化 物（例如氫氧化鈉（NaOH))之群之鹼來適宜地調整。 較佳地’ -或多個乾燥器係串聯連接，其開放實施該等 乾燥器之逐批再生。用於再生之閉環可連續地連接至準備 用於再生其乾燥劑之氣體乾燥器。 本發明之-實施例為-種如上述之用於純化富二氧化碳 煙道氣之系統，其中該系統係以逐批式方式操作。 逐批式操作之-優點為該系統可經最優化且輸入至該系 統十之總熱量因製程順序最優化而減少。 本發明之-目標係提供—種用於純化在於含氧氣體之存 在下燃燒燃料之鍋爐中所產生之氧化碳煙道氣除去污 染物之方法，其包括以下之步驟序列： a) 藉由在共吸附N0x下將水吸附至乾燥器床而乾燥富二 氧化碳煙道氣； b) 自該整體製程隔離該乾燥器； Ο藉由將該乾燥ϋ連接至該閉環使再生環路之壓力均 162823.doc • 6 · 201245639 衡，藉此使實質量之N〇X氣體自乾燥劑解吸； d) 提高該乾燥器之溫度，藉此使水蒸氣自該乾燥劑解 吸； e) 在含有洗滌介質之滌氣塔中洗滌負載水及Ν〇χ之再生 氣體，藉此移除NOx氣體及使水蒸氣凝結至該洗滌介質 中； f) 藉由用來自該經乾燥製程流之富eh氣體再充填該系 統來冷卻經再生之乾燥器並排放潮濕的再生氣體； g) 當冷卻步驟完成時使該乾燥器與該閉環隔離； h) 利用該經乾燥製程氣體再加壓該乾燥器至製程壓力； 及視情況 1)在另一乾燥器床負載時使該經再生之乾燥器上線操 作。 步驟1)係在兩個或更多個乾燥器以_聯或並聯方式連接 之情況下（如圖3所示）進行。 步驟m)中’該乾燥器之壓力較佳為約3〇至4〇巴。 本發明之一實施例為上文所述之方法，其中該洗滌步驟 e)包括以下步驟序列： ei)排放過剩氣體以保持受熱系統中之壓力； eii)使用鼓風機或壓縮機補償該系統中之壓力損耗來提 高該等再生氣體之壓力； em)在移除水及NOx之後再加熱該等再生氣體； eiv)將貫質上不含水蒸氣及污染性Ν〇χ氣體之該煙道氣 再引入該乾燥器；及 162823.doc 201245639 ev)當完成解吸步驟時隔離該洗滌塔。 在本發明之一實施例中提供一種如上述之方法，其中藉 由排放過剩氣體保持該受熱系統中之壓力於適宜水平而保 持該壓力。 ’、 在本發明方法之-實施例中，可增加料再生氣體之壓 力。可藉由採用適宜構件補償該系統之厘力損耗來增加該 壓力適宜之構件可為（例如）鼓風機或壓縮機。 根據該方法之-實施例，在移除水及Ν〇χ之後加熱該等 再生氣體》 二後’將實質上不含水蒸氣及污染性NOx氣體之煙道氣 再引入該乾燥器。 於最、、的解吸步驟之後n條氣塔與該閉環+所包括 之乾燥器隔離。 _本發月< |施例為—種方法，其中在步驟之壓力均 衡之前使該閉環保持在約15至25巴之壓力下。 在該縣氣塔中循環之絲介質為水，視情況將其pH調整 為約5。可藉由添加鹼（通常為選自數⑽3)或氮氧化納 (NaOH)之鹼）來調整該pH。 本發月之f施例為一種方法，其中經解吸之 塔中冷凝，併入該洗條介質巾。 在本發明方法之-實施例中，其中該壓力鹤持在約2 巴以上’較佳保持在約1〇巴以上。 該方法之-優點為可使降壓期間因低溫所引起之乾燥劑 162823.doc 201245639 上迎万法之步驟c)亦可包括將再生煙道氣加熱，較佳達 16〇至23 0°C之溫度之步驟。 此外，該方法可包括其中可s w 丹甲了另外使步驟d)中該煙道氣之 溫度升高以自乾燥器除去水之舟 八之步驟。然而，該溫度應保持 在160至230°C之區間》 【實施方式】 現將參照附圖更詳細地描述本發明。 用於再生之氣體可包括作為、专选 #馬巧·染物之惰性氣體（諸如 C〇2、N2、〇2、AD與煙道氣及蒸汽之混合物。 在蒸汽冷凝為液體之步驟中’重點係保持壓力為至少1〇 巴:此係藉由添加惰性氣體，較佳藉由在再生氣體鼓風機 之前添加該惰性氣體來達成。 圖1為鋼爐系統1自其側面觀察之音 _ 规脊' 炙不意性表不。該鍋爐系 統1包括作為主要組件之鋼爐2(此實施例中為氧 爐）、蒸汽滿輪發電系統（示意性地表示為4)及氣體清潔= 統6。錢體清潔系統6包括可例如為織物過濾器或靜電集 塵器8之顆粒移除裝置及可為渔式洗務塔1〇之二氧化硫移 除系統。 將諸如煤、油或泥炭之燃料裝納於燃料儲槽12中，且可 丄由供應官14供應至該锅爐2。氧氣來源16可以本身習^ ^方式操作來提供氧氣。該氧氣來源16可為可操作以自* 乳刀離出氧氣之空氣分離裝置、氧氣分離薄膜、储槽或任 ^其他用於提供氧氣至該鍋爐系統〖之來源。供應管道Μ 可操作以推送所產生之氧氣（通常含有9〇至99.9體積％^氣8 I62823.doc 201245639 〇2)至該鍋爐2。管道20可操作以抽 卞乂推送包含二氧化碳之再循 環煙道氣至該鍋爐2。如圖 搶^ μ ^人 不，該供應管道18係於該鍋 爐2之上游接合於該管道2〇，以致氧氣人 再循環煙道氣可在該鍋爐2 /、 3 一 反 上游彼此混合形成通常包含 約20至50體積。/。氧氣，其餘主 _ 、要為一氧化碳與水蒸汽之氣 體混合物。因幾乎沒有允备 — 訂又有4進入該鋼爐2,故幾乎沒有氮 氣供應至該鋼爐2。在實降趨於士 貫際操作中，供應至該鍋爐2之氣體 積體之3體積％以下為空氣，其 丹王要係以空氣洩漏形式經 由（例如）該鋼爐2及該氣體清潔系統6進入該鋼爐系⑹。該 鋼爐2可操作’以在待經由管道2〇供應之與包含二氧化碳 之再循環煙道氣混合之氧氣之存在下燃燒待經由供應管Μ 供應之燃料。蒸汽管22可操作，以推送將於鋼爐2中由於 燃燒所產生之蒸汽至蒸汽渴輪發電系統4，該系以可操作 而以電力形式產生功率。 管道24可操作以推送該鍋爐2中所產生之富二氧化碳煙 道氣至除塵裝m謂「富二氧化碳煙道氣」意指經由 管道24離開該鍋爐2之煙道氣將包含至少4〇體積。/❶之二氧 化碳C〇2。通常，離開該鍋爐2之煙道氣之5〇體積％以上將 為二氧化碳。通常，離開鍋爐2之煙道氣將包含5〇至8〇體 積％之二氧化碳。「富二氧化碳煙道氣」之剩餘物將為約 15至40體積％水蒸氣（H2〇)、2至7體積。/。氧氣（ο*因鍋爐2 中有少許過量的氧氣通常為較佳）及總計約〇至1〇體積％之 其他氣體（主要包括氮氣（NO及氬氣（Ar)，因幾乎無法完八 避免空氣之一些洩漏）。 162823.doc 201245639 該鍋爐2中所產生之富二氧化碳煙道氣通常可包含呈（例 如）塵粒、鹽酸11(^、硫氧化物s〇x及重金屬（包括汞Hg)形 式之污染物’其應在處置二氧化碳之前自該富二氧化碳煙 道氣至少部分地移除。 。亥除塵衮置8移除該虽二氧化碳煙道氣中之大多數塵 粒。。管道26可操作以推送該富二氧化碳煙道氣自該織物過 濾器8至該氣體清潔系統6之該溼式洗滌塔1〇。該溼式洗滌 塔1〇包括循環泵28，其可操作以使包含例如石灰石之吸收 液於漿液循環管30中自該溼式洗滌塔1〇之底部循環至配置 在該渥式洗滌塔10之上部之一組喷嘴32。該等衆液噴嘴U 可操作以精細地分佈該溼式洗滌塔〗〇中 現該吸收液與經由該管道26推送至該渥式洗蘇=之= 氣之間的良好接觸，且以實質上垂直向上之方式在該溼式 洗務塔内部流動，而實現自該富二氧化碳煙道氣有效移 除一"氧化硫S〇2及其他酸性氣體6 經至少部分清潔之富：氧化碳煙道氣經由推送該煙道氣 至氣體分流點36之管道34離開該溼式洗滌塔1〇，在分流點 36處該經至少部分清潔之富二氧化碳煙道氣分為兩股流·， 即經由管道20再循環回至該鍋爐2之第一股流’及經由管 道38推送至呈誠爐系統R氣體壓縮及純化單元（咖)4〇 形式之氣體純化系統之第二股流。在該㈣牝中，該⑼ 潔之富二氧化碳煙道氣經進—步清潔且壓縮以進行處理: 經壓縮之二氧化碳因此經 開進行處理，此有時稱為 由管道41離開該GPU 40且輸送離 「C〇2隔離」。經由管道20再循環 162823.doc •11· 201245639 回至該鍋爐2之該第一股流通常佔離開該溼式洗滌塔⑺之 肩’X 4刀/月潔之畐二氧化碳煙道氣之總流量之5 〇至乃體積 %。通常佔離開該溼式洗滌塔10之該經部分清潔之富二氧 化碳煙道氣總流量之25至50體積％之第二股流因此經由該 官道38推送至該GPU 40，其將更詳細描述於下文。 圖2更詳細地繪示該GPU 40。應明瞭圖2之繪示為示意 性’ GPU可包括用於氣體純化之其他裝置等。 該GPU 40包括至少一個壓縮機’其具有至少一個（及通 常二至十個）用於壓縮該經清潔之富二氧化碳煙道氣之壓 縮階段。各壓縮階段可經配置為分離單元。替代地，及如 圖2例示說明，可藉由共同的驅動器來操作若干個壓縮階 段。圖2之該GPU 40包括具有第一壓縮階段42、第二壓縮 階段44及第三壓縮階段“之壓縮機4〇,。該等第一至第三壓 縮階段42、44、46共同組成該GPU 40之低壓壓縮單元48。 §亥等壓縮階段42、44、46係連接至藉由該壓縮機4〇,之馬達 52驅動之共同傳動軸5〇。 該GPU 40可包括至少一個氣體純化系統中間冷卻。該 GPU 40亦可包括配置於該等壓縮階段42、44、牝中之一者 下游之汞吸附單元54。在圖2之實施例中，該汞吸附單元 54係配置於該第三壓縮階段46之下游，即該低壓壓縮單元 48之下游。應明瞭該汞吸附單元54亦可配置於該第一壓縮 階段42之下游’或該第二壓縮階段44之下游。亦可在該 GPU中配置1個以上之乘吸附單元54，例如位於該第二壓 縮階段44下游之汞吸附單元及位於該第三壓縮階段46下游 162823.doc 12 201245639 之汞吸附單元54。再者，亦可配置一中間冷卻單元56，其 具有該中間冷卻及采吸附單元5 4之中間冷卻功能然缺乏其 之采吸附功能’其位於無中間冷卻及采吸附單元5 4配置於 其下游之該等壓縮階段中之一些或全部之下游。因此，中 間冷卻單元56可配置於圖2之該GPU 40之該等第一及第二 壓縮階段42及44之下游。一此種選用的中間冷卻單元56例 示說明於該第一壓縮階段42之下游。 該經清潔之富二氧化碳煙道氣經由管道38進入該Gpu 4〇 且經引入至該第一壓縮階段42中。管道58視情況經由該中 間冷卻單元56推送該經壓縮氣體自該第一壓縮階段42至該 第二壓縮階段44。管道60視情況經由未顯示之中間冷卻單 元推送該經壓縮氣體自該第二壓縮階段44至該第三壓縮階 4又4 6笞道6 2推送經壓縮氣體自該第三壓縮階段4 6至該中 間冷卻及汞吸附單元54。 /亥水吸附單几54之主要部件為采吸附器％及氣體乾燥器 早疋70。該汞吸附器操作以移除該經壓縮氣體之汞含量中 之至少一部分。 該氣體乾燥器單元7G係用以移除該經壓縮富叫煙道氣 之水蒸氣含量之至少—部分。該氣體乾燥器單元之該等部 件將參照圖3更詳細地描述於下文。 該氣體乾燥料元7G包括〜❹個串聯或並聯連接之氣 體乾燥器(如圖3所示)。不論何種系統，其各顯示如下特 徵：可將至少一個乾燥器移出操作(圖3中係將乾燥器75移 出操作）’同時該等其他乾燥器中之至少一乾燥器(圖3中之 162823.doc 201245639 乾燥器78)係在線來確保連續操作。 該等乾燥器包含刺於自該富二氧化碳煙道氣中吸收水 之乾燥劑。任何乾燥劑皆適用於本發明之系統及方法，較 佳的乾燥劑可選自分子篩、矽膠、沸石及其等效物。 連接至忒（等）氣體乾燥器者為用於再生乾燥劑之閉環 80 〇 包含水蒸氣、濕煙道氣及微量污染物之經清潔之富二氧 化碳煙道氣經由管道67進人該GPU4q。該煙道氣經推送通 過該乾燥器。 該管道67推送該煙道氣至分流點。 /亥管道82推送包含水蒸氣及Ν〇χ氣體之該煙道氣至該滌 乳4 84 ’其中該氣體會遇絲介f返送流1洗務介質 (例如具有經調整pH之水）經由諸如泵之適宜構件％饋送至 該滌氣塔之頂部。經由再循環冷卻器94調節溫度。該洗滌 介質亦可經由管道91自該洗料路推送至廢水處理。負載 水之乾燥器係依照如下步驟序列進行再生： a) 藉由將水吸附至乾燥器床來乾燥富二氧化碳煙道氣； 該乾燥器75經水負載達到吸附限度，此點亦為再生程序之 起始點，於此點，該乾燥器亦因共吸附而負載]^〇父； b) 藉由關閉閥69使該乾燥器與圖2所述之製程隔離； c) 藉由打開未圖示之閥使該乾燥器與該閉環連接來使該 再生環路壓力均衡，藉此該等而讀體部分地自乾燥劑解 吸；該等ΝΟχ氣體經由管道82推送至該滌氣塔84 ; d) 提高該乾燥器75之溫度’藉此自乾燥劑解吸出水蒸 162823.doc 201245639 氣，L 3經解吸水蒸氣之煙道氣經由該管道82推送至該滌 氣塔84 ; e)在含有洗滌介質之該滌氣塔84中洗滌經負載水及 之再生乳體’藉此該等⑻讀體經移除及水蒸氣冷凝至該 洗務介質中； ei)排放過剩的氣體以保持受熱系統中之壓力； eii)使用鼓風機或壓縮機補償該系統中之壓力損耗來增 加該等再生氣體之再循環部分之壓力； ΗΠ)在移除水及Ν〇χ之後，於該再生加熱器附再加献 該等再生氣體； … eiv)將實質上不含水蒸氣及污染性NQx氣體之該煙道氣 於該管道87中推送而再引入至該乾燥器； 、 ev)當完成解吸步驟時藉由關閉閥來隔離該滌氣塔； 0藉由用來自該經乾燥製程流並經由管道8 7推送之富 co2氣體再充填㈣統來使該經再生之乾燥器75冷卻 放出濕再生氣體； g)當完成該冷卻步驟時藉由關閉閥(未圖示)來隔離該乾 燥器； 利用該經乾燥製程氣體再次加壓該乾燥器75達到總體 製程之壓力，較佳達到30至40巴之壓力； Ο在另-乾燥器床負载時使該經再生乾燥器上線操作。 洗‘ ’I貝之pH係藉由添加通常選自氨（ΝΑ)、苛性蘇打 (NaOH)之鹼來調整’然該列表並非巨細靡遺。 該管道包括位於乾燥器之前之用於使該再生氣體乾燥器 I62823.doc -15- 201245639 單元80與該管⑽連接或斷開之閱。 車乂佳地冑氣體分流點置於該乾燥器75之前。 該再生煙道氣經由昝、音 官道82自該氣體乾燥器75推送至滌氣 塔單元。 在該條氣塔8 4中， (經由管道82)並返送 滌介質。 該再生煙道氣係於吸附器之底部引入 回流在該氣體乾燥器之頂部引入之洗 ^邮^丨買鞛由再循環泵92於一環路中再循 環。經由再循環冷卻系統94調整該洗條介質之溫度。通過 蘇氣塔之該洗務介質可經由管道91推送至另一廢水處理。 自滌氣塔返送回至乾燥器之再生煙道氣包含—些量之氮 氧化物氣體與水蒸汽及一些量之氮氧化物氣體。 視隋況藉由氣體鼓風機、壓縮機或其他類似構件使來自 滌氣塔之再生煙道氣再循環至該乾燥器。 …、:後通過省乾燥器單元70之再生煙道氣經輸送至該 GPU之C〇2液化單元及/或其他單元。 該氣體乾燥器單元75當經由管道67連接至該製程時係保 持在較操作該再生閉環者高之壓力下。在將該再生閉環如 連接至該氣體乾燥器之前，該氣體乾燥器單元75及該製程 中所保持之壓力為約3〇至40巴。 包括該氣體乾燥器75及該所連接再生閉環8〇之系統係保 持在〗5至25巴之壓力下。 氮氧化物氣體以實質上與推送至再生環路之該第—組分 相等的量釋放。 I62823.doc 201245639 可將自該氣體乾燥器單元中之该等乾燥器推送之再生氣 體與自該滌氣塔再循環之氣體組合。 管道72將已自其中移除其汞含量之至少一部分及水蒸氣 含量之至少大部分之壓縮氣體自該乾燥器單元7〇推送至該 GPU 40(如圖2所示）之選用的其他單元。該GPu 4〇之該等 選用其他單元之實例包括不可凝結氣體移除單元，例如 C〇2液化單元73，其中該氣體在通常稱為冷卻箱之熱交換 器中冷卻，致使二氧化碳液化而使得該二氧化碳可與在一 如二氧化碳之該溫度下無法液化之氣體（諸如氮氣）分離。 此外，該GPU 40可包括高壓壓縮單元74，其相對二氧化碳 之輸送方向所觀察配置於該C〇2液化單元73之下游，且包 括一或多個用於壓縮該二氧化碳至適宜隔離壓力之壓縮階 段。在該高壓壓縮單元74中之氣體壓縮之後，可呈超臨界 或液體狀態之該經壓縮二氧化碳經由管道4丨推送至c 〇 2隔 離部位76。 圖4顯示用於包括2個乾燥器之Ν〇χ移除系統之先前㈣ 系統。當該系統中之該氣體乾燥器丨12欲進行再生時，藉 由閥使其與該製程系統斷開。使再生煙道氣與水蒸氣^ 離。該水蒸氣經冷凝且經由管道126推送進行進一步之廢 水處理。 該再生煙道氣自言亥乾燥器112經由管道122推送至再生氣 體刀離盗124’ 4分離器124經由管道連接至用於分離 風體之早TtmfDeNQx單元）。料NC)X氣體在其#藉由可 為催化性之製程轉化為氮氣。在分離該等Ν〇χ氣體期間， 162823.doc •17- 201245639 釋放出導致再生廢氣中之濃度峰之氣體。在針對該乾燥器 112之處理、降壓及沖洗時’於最終的再生後，經處理流 之€〇2有損耗。該損耗量可高達3% C02。 儘官已參照許多較佳實施例論述本發明，然孰 關技藝者當明瞭在不脫離本發明之範圍下，可：出多= 變且可以等效物替代其要件。此外，可在不脫離其基本範 圍下作出多種修改以使特定情境或材料適應於本發明之教 不。因此’希望本發明不受限於經揭示為據認為用於實施 本發明之最佳模式之特；t實施例，反之本發明將包括屬於 隨附申請專利範圍之範相之所有實施例。此外，使用術 【圖式簡單說明】 。。第一、第二等並不表示任何順序或重要性，而是該等術 語第一、第二等係用於區別—個要件與另一者。 圖1為鍋爐系統之示意性側視圖。 圖2為氣體壓縮及純化單元之示意性側視圖。 圖3為具有閉環之氣體乾燥器單元之示純側視圖。 圖4為先前技術再生單元之示意性側視圖。 【主要元件符號說明】 1 鋼爐系統 2 銷爐 4 蒸汽渦輪發電系統 6 氣體清潔系統 8 靜電集塵器 10 溼式洗滌塔 162823.doc 201245639 12 燃料儲槽 14 供應管 16 氧氣來源 18 供應管道 20 管道 22 蒸汽管 24 管道 26 管道 28 循環泵 30 漿液循環管 32 漿液噴嘴 34 管道 36 氣體分流點 38 管道 40 氣體壓縮及純化單元（GPU) 40' 壓縮機 41 管道 42 第一壓縮階段 44 第二壓縮階段 46 第三壓縮階段 48 低壓壓縮單元 50 傳動轴 52 馬達 54 汞吸附單元 162823.doc -19- 201245639 56 中間冷卻單元 58 管道 60 管道 62 管道 66 汞吸附器 67 管道 70 氣體乾燥器單元 72 管道 73 C02液化單元 74 高壓壓縮單元 75 乾燥器 76 C02隔離部位 78 乾燥器 80 閉環 82 管道 84 滌氣塔 86 再生加熱器 87 管道 91 管道 92 再循環泵 94 再循環冷卻系統 112 氣體乾燥器 122 管道 124 再生氣體分離器 162823.doc -20- 201245639 125 126201245639 VI. DESCRIPTION OF THE INVENTION: TECHNICAL FIELD OF THE INVENTION The present invention generally relates to the reduction of nitrogen oxides from flue gases. DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a desiccant regeneration system for low enthalpy emissions. The invention further relates to a method of regenerating a desiccant having a low emission. [Prior Art] In a combustion plant such as a power plant, a hot process gas is generated during combustion of a fuel such as a medium, oil, peat, waste, etc., and the process gas contains, in particular, carbon dioxide C〇2. With increasing environmental demands, a variety of processes have been developed to remove carbon dioxide from process processes. An example of such a process is the so-called oxy-fuel process. In an oxy-fuel process, a fuel such as one of the above fuels is combusted in the presence of a lean nitrogen gas. Carbon dioxide-rich flue gas is produced in the oxygen-fuel combustion process and can be disposed of to reduce carbon dioxide emissions. The carbon dioxide rich flue gas may also contain a polluting gas such as NOx gas. These contaminants should also be removed. There are a number of different methods for removing nitrogen oxides from the gas stream, for example, by using Gpu off-gas or by using so-called DeN〇x units, which are removed by catalytic reduction. US 6 146 605 discusses methods for reducing flue gas, such as selective catalytic reduction (SCR) and selective non-catalytic reduction, and combinations thereof. Gas _3) is used herein as a reducing gas to remove the NOx gases. The system is not connected to the system for regenerating the dry_. In (10) 4 533 365, a gas containing N〇x gas 162823.doc 201245639 is separated by molecular sieve and recycled to the system. In the desiccant regeneration system used in the past, contaminants such as helium gas are co-adsorbed. When the desiccant is subsequently regenerated, the gas is also released, which causes an unfavorable concentration peak in the regenerated exhaust gas. There is therefore a need to solve the problem to avoid emissions or substantially avoid NOx emissions during desiccant regeneration. SUMMARY OF THE INVENTION One object of the present invention is to provide a system for purifying a carbon dioxide-rich flue gas produced in a boiler containing an oxygen-containing gas in which a fuel is burned and contaminated with helium gas. An embodiment of the invention is a system for purifying a carbon dioxide-rich flue gas produced in a boiler that burns fuel in the presence of an oxygen-containing gas and contaminated with helium gas, wherein the system comprises: one or more a gas dryer comprising a desiccant for removing at least a portion of the water content of the further compressed carbon dioxide rich flue gas; a closed loop of the desiccant for regenerating the dryers connected to the dryers Wherein the χ0 χ gas is removed from the water vapor substantially separately. The system according to the invention produces only a low regeneration exhaust stream, which is environmentally friendly. In addition, the emission of antimony is also reduced compared to known methods and the peak emissions of helium gas are also avoided by the system. The m point of the system is a reduction in the amount of (3) 2, and in the system according to the invention, the amount of loss is less than 〇2 volume 〇 / 〇. An embodiment of the invention is a system for purifying flue gas as described above (4), wherein the closed loop comprises a strip of detergent medium operable to absorb NOx gas removed from the dryer during the regeneration period 162823.doc 201245639 Gas tower. An embodiment of the invention is a system for purifying a carbon dioxide rich flue gas as described above, wherein water desorbed from the dryer will be condensed in the scrubber. In a system for purifying a carbon dioxide rich flue gas according to the present invention, wherein the pH of the scrubbing medium can be suitably adjusted to maximize the scrubbing of the gas. An embodiment of the invention is a system for purifying carbon dioxide-rich flue gas, wherein the pH is obtained by adding a group selected from the group consisting of ammonia (3) and an alkali metal hydroxide (such as sodium hydroxide (NaOH)). The base is suitably adjusted. Preferably, the - or plurality of dryers are connected in series, which is open for batch-to-batch regeneration of the dryers. The closed loop for regeneration can be continuously connected to a gas dryer ready to regenerate its desiccant. An embodiment of the invention is a system for purifying carbon dioxide rich flue gas as described above, wherein the system is operated in a batch mode. Batch-to-batch operation - the advantage is that the system can be optimized and the total heat input to the system is reduced due to process sequence optimization. The present invention is directed to a method for purifying oxidized carbon flue gas generated in a boiler for burning fuel in the presence of an oxygen-containing gas to remove contaminants, comprising the following sequence of steps: a) by Co-adsorbing N0x to adsorb water to the dryer bed to dry the carbon dioxide rich flue gas; b) isolating the dryer from the overall process; Ο by connecting the dry crucible to the closed loop, the pressure of the regeneration loop is 162,823. Doc • 6 · 201245639 balance, whereby the mass of N〇X gas is desorbed from the desiccant; d) increasing the temperature of the dryer, thereby desorbing water vapor from the desiccant; e) Washing the water and the regeneration gas of the helium in the gas column, thereby removing the NOx gas and condensing the water vapor into the washing medium; f) refilling the system by using the rich eh gas from the dried process stream Cooling the regenerated dryer and discharging the humid regeneration gas; g) isolating the dryer from the closed loop when the cooling step is completed; h) repressurizing the dryer to the process pressure by using the dried process gas; Happening 1) The regenerated dryer is operated on-line while another dryer bed is being loaded. Step 1) is carried out in the case where two or more dryers are connected in a _ joint or a parallel connection (as shown in Fig. 3). In step m), the pressure of the dryer is preferably from about 3 Torr to about 4 Torr. An embodiment of the invention is the method described above, wherein the washing step e) comprises the following sequence of steps: ei) discharging excess gas to maintain pressure in the heated system; eii) compensating the system using a blower or compressor Pressure loss to increase the pressure of the regeneration gas; em) reheating the regeneration gas after removal of water and NOx; eiv) reintroducing the flue gas of the non-aqueous vapor and polluting helium gas The dryer; and 162823.doc 201245639 ev) isolating the scrubber when the desorption step is completed. In one embodiment of the invention there is provided a method as described above, wherein the pressure is maintained by discharging excess gas to maintain the pressure in the heated system at an appropriate level. In the embodiment of the method of the invention, the pressure of the feed regeneration gas can be increased. The means for increasing the pressure by compensating the force loss of the system with suitable components may be, for example, a blower or a compressor. According to an embodiment of the method, the regeneration gas is heated after the removal of water and helium, and then the flue gas substantially free of water vapor and contaminating NOx gas is reintroduced into the dryer. After the most desorption step, the n gas columns are isolated from the drier included in the closed loop +. The present invention is a method in which the closed loop is maintained at a pressure of about 15 to 25 bar before the pressure equalization of the steps. The silk medium circulating in the gas tower of the county is water, and its pH is adjusted to about 5 as the case may be. The pH can be adjusted by adding a base (usually a base selected from the number (10) 3) or sodium oxynitride (NaOH). The present embodiment is a method in which the desorbed column is condensed and incorporated into the strip medium. In an embodiment of the method of the invention wherein the pressure crane is maintained above about 2 bar' preferably maintained above about 1 bar. The method has the advantage that the desiccant can be caused by low temperature during the depressurization period. 162823.doc 201245639 The step c) of the method can also include heating the regenerated flue gas, preferably up to 16 〇 to 23 0 ° C. The step of temperature. Additionally, the method can include the step of additionally singing the temperature of the flue gas in step d) to remove water from the dryer. However, the temperature should be maintained in the range of 160 to 230 ° C. [Embodiment] The present invention will now be described in more detail with reference to the accompanying drawings. The gas used for regeneration may include as an inert gas of the selected #马巧· dyes (such as C〇2, N2, 〇2, AD and a mixture of flue gas and steam. In the step of vapor condensation into a liquid] Maintaining a pressure of at least 1 bar: this is achieved by adding an inert gas, preferably by adding the inert gas before the regeneration gas blower. Figure 1 shows the sound of the steel furnace system 1 viewed from its side. The boiler system 1 includes a steel furnace 2 (an oxygen furnace in this embodiment) as a main component, a steam full-wheel power generation system (shown schematically as 4), and a gas cleaning system 6. The cleaning system 6 includes a particulate removal device that can be, for example, a fabric filter or electrostatic precipitator 8 and a sulfur dioxide removal system that can be a fishing scrubber. A fuel such as coal, oil or peat is contained in the fuel. The reservoir 12 is, and may be supplied, by the supply officer 14 to the boiler 2. The oxygen source 16 may operate in its own manner to provide oxygen. The oxygen source 16 may be operable to evacuate oxygen from the ... Air separation unit, oxygen separation membrane, storage Or any other source for supplying oxygen to the boiler system. Supply piping Μ operable to push the generated oxygen (usually containing 9 to 99.9 vol% of gas 8 I62823.doc 201245639 〇 2) to the boiler 2 The pipe 20 is operable to pump the recycled flue gas containing carbon dioxide to the boiler 2. The supply pipe 18 is coupled to the pipe 2 upstream of the boiler 2, as shown in the figure. Thus, the oxygen human recycle flue gas can be mixed with each other upstream of the boiler 2 /, 3 to form a gas mixture which usually contains about 20 to 50 volumes of oxygen, and the remaining main _ is a gas mixture of carbon monoxide and water vapor. There is no allowance - there is 4 entering the steel furnace 2, so almost no nitrogen is supplied to the steel furnace 2. In the actual operation, the volume of the gas volume supplied to the boiler 2 is less than 3% by volume. In the case of air, the king of the king enters the steel furnace (6) in the form of an air leak via, for example, the steel furnace 2 and the gas cleaning system 6. The steel furnace 2 is operable to supply the supply to be supplied via the pipeline 2 Recycled flue containing carbon dioxide The fuel to be supplied via the supply pipe 燃烧 is combusted in the presence of gas mixed oxygen. The steam pipe 22 is operable to push steam generated in the steel furnace 2 due to combustion to the steam thirst power generation system 4, which is operable The power is generated in the form of electricity. The pipe 24 is operable to push the carbon dioxide rich flue gas generated in the boiler 2 to the dust removal device m, which is referred to as "carbon dioxide rich flue gas" means the flue gas exiting the boiler 2 via the pipe 24. It will contain at least 4 volumes of carbon dioxide C. 2. Typically, more than 5% by volume of the flue gas leaving the boiler 2 will be carbon dioxide. Typically, the flue gas leaving the boiler 2 will contain 5 to 8 〇% by volume of carbon dioxide. The remainder of the "carbon dioxide rich flue gas" will be about 15 to 40% by volume water vapor (H2 〇), 2 to 7 volumes. /. Oxygen (ο* is usually preferred due to a slight excess of oxygen in boiler 2) and other gases totaling approximately 1% by volume (mainly including nitrogen (NO and argon (Ar), as it is almost impossible to avoid air) Some leaks.) 162823.doc 201245639 The carbon dioxide-rich flue gas produced in this boiler 2 can usually be in the form of, for example, dust particles, hydrochloric acid 11 (^, sulfur oxides s〇x and heavy metals (including mercury Hg). The contaminant 'which should be at least partially removed from the carbon dioxide rich flue gas prior to disposal of the carbon dioxide. The dust removal device 8 removes most of the dust particles in the carbon dioxide flue gas. The conduit 26 is operable to The carbon dioxide rich flue gas is pushed from the fabric filter 8 to the wet scrubber 1 of the gas cleaning system 6. The wet scrubber 1 comprises a circulation pump 28 operable to contain, for example, limestone absorption The liquid is circulated from the bottom of the wet scrubber 1 to the bottom of the wet scrubber 1 to a group of nozzles 32 disposed above the scrubber 10. The liquid nozzles U are operable to finely distribute the wet Washing tower The absorbing liquid is in good contact with the gas fed through the conduit 26 to the sputum, and flows inside the wet scrubbing tower in a substantially vertical upward manner, thereby realizing the carbon dioxide-rich smoke The gas effectively removes a "sulphur oxide S〇2 and other acid gases 6 that are at least partially cleaned: the carbon oxide flue gas leaves the wet scrubber via a conduit 34 that pushes the flue gas to the gas split point 36 1〇, at the split point 36, the at least partially cleaned carbon dioxide rich flue gas is split into two streams, ie, recirculated back to the first stream of the boiler 2 via line 20 and pushed through conduit 38 to The second stream of the gas purification system in the form of a gas compression and purification unit (Caf) of the furnace system. In the (4), the (9) clean carbon dioxide flue gas is cleaned and compressed for processing. : The compressed carbon dioxide is therefore treated by opening, which is sometimes referred to as leaving the GPU 40 by conduit 41 and transported away from "C〇2." Recirculation via line 20 162823.doc •11· 201245639 Back to the boiler 2 The first stream usually takes off The total flow of the carbon dioxide flue gas of the shoulder of the wet scrubber (7) is 5 〇 to 5% by volume. Usually the partially cleaned carbon dioxide-rich smoke leaving the wet scrubber 10 A second stream of 25 to 50% by volume of the total flow of the gas is thus pushed to the GPU 40 via the official track 38, which will be described in more detail below. Figure 2 illustrates the GPU 40 in more detail. Illustrated as 'the GPU may include other devices for gas purification, etc. The GPU 40 includes at least one compressor' having at least one (and usually two to ten) for compressing the cleaned carbon dioxide-rich smoke The compression phase of the road. Each compression stage can be configured as a separation unit. Alternatively, and as illustrated in Figure 2, several compression stages can be operated by a common driver. The GPU 40 of FIG. 2 includes a compressor having a first compression phase 42, a second compression phase 44, and a third compression phase. The first to third compression phases 42, 44, 46 together comprise the GPU. The low pressure compression unit 48 of 40. The compression stages 42, 44, 46 are connected to a common drive shaft 5〇 driven by the motor 52 of the compressor 4. The GPU 40 may include at least one gas purification system intermediate Cooling. The GPU 40 can also include a mercury adsorption unit 54 disposed downstream of one of the compression stages 42, 44, and a crucible. In the embodiment of FIG. 2, the mercury adsorption unit 54 is configured for the third compression. Downstream of stage 46, downstream of the low pressure compression unit 48. It should be understood that the mercury adsorption unit 54 can also be disposed downstream of the first compression stage 42 or downstream of the second compression stage 44. Also in the GPU. More than one multiplying adsorption unit 54 is disposed, for example, a mercury adsorption unit located downstream of the second compression stage 44 and a mercury adsorption unit 54 located downstream of the third compression stage 46 162823.doc 12 201245639. Further, a mercury adsorption unit 54 may be disposed. Intermediate cooling unit 56 having The intermediate cooling function of the intermediate cooling and extraction unit 54 lacks its adsorption function 'which is located downstream of some or all of the compression stages in which there is no intermediate cooling and the adsorption unit 54 is disposed downstream. The intermediate cooling unit 56 can be disposed downstream of the first and second compression stages 42 and 44 of the GPU 40 of FIG. 2. An optional intermediate cooling unit 56 is illustrated downstream of the first compression stage 42. The cleaned carbon dioxide rich flue gas enters the Gpu 4 via conduit 38 and is introduced into the first compression stage 42. The conduit 58 optionally pushes the compressed gas from the first compression stage via the intermediate cooling unit 56. 42 to the second compression stage 44. The conduit 60, as the case may be, pushes the compressed gas from the second compression stage 44 to the third compression stage 4 and the fourth stage 6 2 via the unillustrated intermediate cooling unit to push the compressed gas From the third compression stage 46 to the intermediate cooling and mercury adsorption unit 54. The main components of the /Hybrid adsorption unit 54 are the adsorber % and the gas dryer early 70. The mercury adsorber operates to shift At least a portion of the mercury content of the compressed gas. The gas dryer unit 7G is for removing at least a portion of the water vapor content of the compressed rich flue gas. The components of the gas dryer unit will This is described in more detail below with reference to Figure 3. The gas drying unit 7G comprises ~ one gas dryer connected in series or in parallel (as shown in Figure 3). Regardless of the system, each of which exhibits the following characteristics: A dryer removal operation (the dryer 75 is removed from operation in Figure 3) while at least one of the other dryers (162823.doc 201245639 dryer 78 in Figure 3) is in-line to ensure continuous operation. The dryers comprise a desiccant that absorbs water from the carbon dioxide rich flue gas. Any desiccant is suitable for use in the system and method of the present invention. Preferred desiccants may be selected from the group consisting of molecular sieves, silicones, zeolites and equivalents thereof. The gas cooler connected to the helium (etc.) is a closed loop for regenerating the desiccant. 80 经 The cleaned rich carbon dioxide flue gas containing water vapor, wet flue gas and trace contaminants enters the GPU 4q via line 67. The flue gas is pushed through the dryer. The conduit 67 pushes the flue gas to the split point. /Hai pipe 82 pushes the flue gas containing water vapor and helium gas to the lotion 4 84 ' wherein the gas will encounter the flow medium 1 (for example, water with adjusted pH) via A suitable component % of the pump is fed to the top of the scrub column. The temperature is adjusted via a recirculating cooler 94. The washing medium can also be pushed from the washing path to the wastewater treatment via line 91. The water-loaded dryer is regenerated according to the following sequence of steps: a) drying the carbon dioxide-rich flue gas by adsorbing water to the dryer bed; the dryer 75 is subjected to a water load to reach the adsorption limit, which is also a regeneration process. Starting point, at which point the dryer is also loaded by co-adsorption; b) isolating the dryer from the process described in Figure 2 by closing valve 69; c) by opening without The valve connects the dryer to the closed loop to equalize the pressure of the regenerative loop, whereby the readers are partially desorbed from the desiccant; the helium gases are pushed to the scrubber 84 via conduit 82; d) Increasing the temperature of the dryer 75 'by desorbing the water from the desiccant 162823.doc 201245639 gas, the flue gas of the L 3 desorbed vapor is pushed to the scrub column 84 via the conduit 82; e) containing the scrubbing medium The scrubber 84 scrubs the loaded water and the regenerated milk body 'by the (8) reading body is removed and the water vapor is condensed into the washing medium; ei) the excess gas is discharged to maintain the heat receiving system Pressure; eii) compensating the system with a blower or compressor Pressure loss to increase the pressure of the recirculating portion of the regenerative gas; ΗΠ) after the water and helium are removed, the regenerative heater is replenished with the regenerative gas; ... eiv) will be substantially free of water The flue gas of the vapor and the contaminating NQx gas is pushed into the pipe 87 and reintroduced into the dryer; ev) isolating the scrubber by closing the valve when the desorption step is completed; The regenerated coagulator 75 is cooled and discharged to the wet regeneration gas by the dry process stream and recharged via the conduit 81; g) by closing the valve (not shown) when the cooling step is completed Isolating the dryer; using the dried process gas to pressurize the dryer 75 again to achieve a pressure of the overall process, preferably at a pressure of 30 to 40 bar; and the regenerative dryer is placed under the load of the other-dryer bed Go online. The pH of the wash is adjusted by adding a base usually selected from the group consisting of ammonia (hydroquinone) and caustic soda (NaOH). However, the list is not superficial. The conduit includes a section prior to the dryer for connecting or disconnecting the regeneration gas dryer I62823.doc -15- 201245639 unit 80 to the tube (10). A turret gas split point is placed before the dryer 75. The regenerated flue gas is pushed from the gas dryer 75 to the scrubber unit via a crucible and an acoustic channel 82. In the gas column 84, (via line 82) and returning the polyester medium. The regenerated flue gas is introduced into the bottom of the adsorber and refluxed. The scrubber introduced at the top of the gas dryer is recirculated by a recirculation pump 92 in a loop. The temperature of the wash strip medium is adjusted via a recirculating cooling system 94. The washing medium passing through the gas tower can be pushed through the conduit 91 to another wastewater treatment. The regenerated flue gas returned from the scrubber tower to the dryer contains a quantity of nitrogen oxide gas and water vapor and some amount of nitrogen oxide gas. The regenerated flue gas from the scrubber is recycled to the dryer by a gas blower, compressor or the like as appropriate. ...,: The regenerated flue gas passing through the dry dryer unit 70 is then delivered to the C〇2 liquefaction unit and/or other unit of the GPU. The gas dryer unit 75 is maintained at a higher pressure than the one operating the regenerative closed loop when connected to the process via line 67. The gas dryer unit 75 and the pressure maintained in the process are about 3 Torr to 40 bar before the regenerative closed loop is connected to the gas dryer. The system including the gas dryer 75 and the connected regenerative closed loop 8 is maintained at a pressure of from 5 to 25 bar. The nitrogen oxide gas is released in substantially the same amount as the first component pushed to the regeneration loop. I62823.doc 201245639 The regeneration gas pushed from the dryers in the gas dryer unit can be combined with the gas recycled from the scrubber. The conduit 72 pushes compressed gas from which at least a portion of its mercury content and at least a substantial portion of the water vapor content has been removed from the dryer unit 7 to other selected units of the GPU 40 (shown in Figure 2). Examples of such other units that are selected for the GPu 4 include a non-condensable gas removal unit, such as a C 〇 2 liquefaction unit 73, wherein the gas is cooled in a heat exchanger, commonly referred to as a cooling box, causing the carbon dioxide to liquefy such that Carbon dioxide can be separated from a gas that cannot be liquefied at such temperatures as carbon dioxide, such as nitrogen. In addition, the GPU 40 can include a high pressure compression unit 74 disposed downstream of the C〇2 liquefaction unit 73 as viewed in the direction of carbon dioxide transport and including one or more compression stages for compressing the carbon dioxide to a suitable isolation pressure. . After the gas in the high pressure compression unit 74 is compressed, the compressed carbon dioxide, which may be in a supercritical or liquid state, is pushed through the conduit 4 to the c 〇 2 isolation site 76. Figure 4 shows a prior (four) system for a helium removal system including two dryers. When the gas dryer 12 in the system is to be regenerated, it is disconnected from the process system by a valve. The regenerated flue gas is separated from the water vapor. The water vapor is condensed and pushed via line 126 for further waste water treatment. The regenerated flue gas is pushed from the whisper dryer 112 via the conduit 122 to the regenerative gas knife detachment 124'4 separator 124 via a pipe to the early TtmfDeNQx unit for separating the wind body). The NC)X gas is converted to nitrogen by its catalytic process. During the separation of the helium gases, 162823.doc •17- 201245639 releases the gas that causes the concentration peaks in the regenerative exhaust gas. At the time of treatment, depressurization and rinsing of the dryer 112, after the final regeneration, the treated stream has a loss of 〇2. This loss can be as high as 3% C02. The present invention has been described with reference to a number of preferred embodiments, and it will be apparent to those skilled in the art that the invention may be substituted and varied. In addition, many modifications may be made to adapt a particular situation or material to the teachings of the invention. Therefore, it is intended that the present invention not be limited to the embodiment of the invention, In addition, use the technique [simple description of the schema]. . The first, second, etc. do not indicate any order or importance, but rather the first, second, etc. of the terms are used to distinguish one element from the other. Figure 1 is a schematic side view of a boiler system. Figure 2 is a schematic side view of a gas compression and purification unit. Figure 3 is a pure side view of a gas dryer unit with a closed loop. 4 is a schematic side view of a prior art regeneration unit. [Main component symbol description] 1 Steel furnace system 2 Pin furnace 4 Steam turbine power generation system 6 Gas cleaning system 8 Electrostatic dust collector 10 Wet scrubber 162823.doc 201245639 12 Fuel tank 14 Supply pipe 16 Oxygen source 18 Supply pipe 20 Pipe 22 Steam pipe 24 Pipe 26 Pipe 28 Circulating pump 30 Slurry circulation pipe 32 Slurry nozzle 34 Pipe 36 Gas split point 38 Pipe 40 Gas compression and purification unit (GPU) 40' Compressor 41 Pipe 42 First compression stage 44 Second compression Stage 46 Third compression stage 48 Low pressure compression unit 50 Drive shaft 52 Motor 54 Mercury adsorption unit 162823.doc -19- 201245639 56 Intermediate cooling unit 58 Pipe 60 Pipe 62 Pipe 66 Mercury adsorber 67 Pipe 70 Gas dryer unit 72 Pipe 73 C02 liquefaction unit 74 High pressure compression unit 75 Dryer 76 C02 Isolation site 78 Dryer 80 Closed loop 82 Pipeline 84 scrubber 86 Regeneration heater 87 Pipe 91 Pipe 92 Recirculation pump 94 Recirculation cooling system 112 Gas dryer 122 Pipe 124 Regeneration Gas separator 162823.do c -20- 201245639 125 126
DeNOx單元 管道 162823.doc -21DeNOx unit pipe 162823.doc -21