附件一：第85111751號專利申請案中文說明書修正夏 民國86年10戶 丨锻正 . 1-- 五、發明説明（1 ) 〆 、續請委貝明示，本案修正後是否^更原實質内^ 經濟部中央標隼局員工消費合作社印製 本發明係關於一種藉由流化作用而從微粒子含氧化鐵 之物質中製造熔融生鐵或液態鋼預產物的方法，其中該含 氧化鐵物貧係在至少一個預還原階段中藉肋於一還原氣體 而預還原，隨後再於最終還原階段中被還原成海綿鐵，在 碳載劑及含氧氣體的供應下該海綿鐵將於熔化一氧化區域 內熔化，同時會產生一可.導入最終還原階段並在那裡反應 、卸下、隨後再導入預還原階段之含C 0 —及H2 —的還 原氣體，同樣地該被導入預還原階段之還原氣體也將在此 反應、卸下、再接受洗滌、隨後則以輸出氣體被帶走；且 其中至少一部份反應過之還原氣體可從c〇2中純化、加 熱 '並再使用做爲供該含氧化鐵物質還原之再循環還原氣 體；本發明同時也係關於實施該方法的設備。 此一形態之方法可由美國專利U S — A - 5 ，1 8 5 ，〇 3 2案號中得知。使用此方法時，爲了使還原氣體之 還原電位及熱能達到最大可能的程度，還原氣體將通過所 有的還原階段及通過在含氧化鐵物質之流動方向中緊接於 前的預加熱階段，並從第一個預加熱階段中抽回而做爲頂 端氣體，隨後再清洗。將一部份頂端氣體壓縮，並使之接 受C〇2消去作用，隨後再加熱。該依此加熱並從C〇2 中純化至較大程度的頂端氣體隨後將以再循環還原氣體送 進還原程序中，藉此，即可利用仍存在頂端氣體內的還原 劑。然而，此處所牽渉的缺點之一是，每一流化床還原階 段及每一預加熱階段必須尺寸化，如此才能運轉所有的氣 體，亦即新製造的還原氣體加上再循環的還原氣體。 (請先聞讀背面之注意事項再ΛΜ頁.) { cns ) A4W (210x297^) . 4 . " 附件一：第85111751號專利申請案中文說明書修正夏 民國86年10戶 丨锻正 . 1-- 五、發明説明（1 ) 〆 、續請委貝明示，本案修正後是否^更原實質内^ 經濟部中央標隼局員工消費合作社印製 本發明係關於一種藉由流化作用而從微粒子含氧化鐵 之物質中製造熔融生鐵或液態鋼預產物的方法，其中該含 氧化鐵物貧係在至少一個預還原階段中藉肋於一還原氣體 而預還原，隨後再於最終還原階段中被還原成海綿鐵，在 碳載劑及含氧氣體的供應下該海綿鐵將於熔化一氧化區域 內熔化，同時會產生一可.導入最終還原階段並在那裡反應 、卸下、隨後再導入預還原階段之含C 0 —及H2 —的還 原氣體，同樣地該被導入預還原階段之還原氣體也將在此 反應、卸下、再接受洗滌、隨後則以輸出氣體被帶走；且 其中至少一部份反應過之還原氣體可從c〇2中純化、加 熱 '並再使用做爲供該含氧化鐵物質還原之再循環還原氣 體；本發明同時也係關於實施該方法的設備。 此一形態之方法可由美國專利U S — A - 5 ，1 8 5 ，〇 3 2案號中得知。使用此方法時，爲了使還原氣體之 還原電位及熱能達到最大可能的程度，還原氣體將通過所 有的還原階段及通過在含氧化鐵物質之流動方向中緊接於 前的預加熱階段，並從第一個預加熱階段中抽回而做爲頂 端氣體，隨後再清洗。將一部份頂端氣體壓縮，並使之接 受C〇2消去作用，隨後再加熱。該依此加熱並從C〇2 中純化至較大程度的頂端氣體隨後將以再循環還原氣體送 進還原程序中，藉此，即可利用仍存在頂端氣體內的還原 劑。然而，此處所牽渉的缺點之一是，每一流化床還原階 段及每一預加熱階段必須尺寸化，如此才能運轉所有的氣 體，亦即新製造的還原氣體加上再循環的還原氣體。 (請先聞讀背面之注意事項再ΛΜ頁.) { cns ) A4W (210x297^) . 4 . " A7 B7 五、發明説明（2 ) 請 先 閱- 讀 背 之， 注 意 事 項 再 V" 頁 在利用C 0 / C 0 2混合物並藉由流化作用的氧化鐵 之還原反應中，在高溫下（例如，超過7 0 0 °c)及較低 還原電位下（亦即還原氣體中增加了（：〇2及Η 2〇含量 )定向、針狀之鐵沈澱物係存在於細礦粒子的表面上。在 流化床中這些鐵沈澱物開始有了'^黏著'現象。隨著非常 高程度的還原反應時，礦石之凝集作用會發生，因此就阻 礙了還原程序。然而，若還原反應係在還原氣體之非常高 或最高的還原電位下進行時，鐵沈澱物將會稠密或多孔， 如此就不會觀察到^黏著'。 本發明之目的在於避免這些缺點及困難，並且提供一 種方法及實施該方法之裝置，彼係經由增加還原氣體之.還 原電位以確保還原反應且不會有*黏著'發生，然而，其 中該利用來製造還原氣體之碳載劑的量並沒有增加：與先 前技藝比較時反而能節省碳載劑。 根據本發明，只要將一部份從最終還原階段流入預還 原階段的還原氣體分開，清洗、從C〇2中純化、並'加熱 之，隨後再循環至最終還原階段，即可達成此一目標。 經濟部中央標準局員工消費合作杜印製 使用如本發明之方法時，正確地是可利用仍存在於該 從最終還原階段出來，並與供另外之還原階段及/或任何 預加熱用之相同還原氣體分開的還原氣體內的還原電位； 從此一事實中正可產生實質的優點： 根據本發明，藉由增加還原氣體的量便可確保高還原 電位，其中，隨著還原程序一步步地進行，僅需在最終還 原階段中提供增量的還原氣體。藉此，在溫度最高且 '黏 本紙張尺度適用中國國家標準（CNS ) A4規格（210X 297公釐） A7 B7 五、發明説明（3 ) 著'危險最大的最終還原階段中可確實地避免"黏著'， 同時也可排除使設備中的所有零件（也就是所有氣體導管 、反應器、壓縮器等）尺寸化的需求；如此，依此方法所 提供之任何預加熱階段及流化床還原階段都可在增量的遼 原氣體中操作。 因此，本發明能選擇性地利用高還原電位，結果，其 他的還原階段就可提供理論上最小量的還原氣體，並且可 使所需設備成比例地變小，因而較不昂貴。 必然地，本發明不僅可以最適當方式使所有設備之零 件尺寸化，亦即盡可能地有最大的生產能力，也盡可能地 只使用最小量的製造還原氣體所需之碳載劑；換句話說， 煤消耗率可減至最低，且同時還可確實地避免任何 ' 黏著 #的危險。再者，儘管煤只能形成不足量的還原氣體，但 在熔化氣化區域中欲使用有高Cfix及低灰份之煤將變得 可行，而仍能達成均勻的熱平衡，亦即，只要將小量的水 加入熔化氣化區域內，便可增加還原氣體的量。 經濟部中央標準局員工消費合作杜印製 V- (請先M-讀背面t注意事項存^本莨) # 由於在最後之還原階段適用非常高的還原電位，所以 一部份從最終還原階段中取出並從相同氣體中分開，而後 再循環至該相同氣體中之還原氣體應加熱至範圍在8 0 0 至9 0 0 °C的還原溫度，舉例之，可加熱至約8 5 0 °C。 較有利地，該從最終還原階段中抽回並分開之還原氣 體可以重複及/或再生之方式，及/或藉由部份燃燒該已 抽回之一部份的還原氣體方式加熱至還原溫度。 較佳地，該加熱之還原氣體的再循環係藉由將其混合 本紙張尺度適用中國國家標準（CNS ) A4規格（210 X297公釐）_ 6 - A7 B7 五、發明説明（4 ) 入從熔化氣化區域出來且已除灰的熱還原氣體中而執行。 爲了將脫離溶化器氣化器之還原氣體冷卻至還原溫度 ，適當部份之從co2純化的還原氣體將以冷卻狀態再循 環，較佳地係在彼等導入最終還原階段之前即先混合入從 熔化氣化區域中離逸的熱還原氣體中。 關於最終還原階段之等易溫度調節，較有利地係先清 洗一部份從熔化氣化區域中出來之熱還原氣體，隨後再以 冷卻狀態與從熔化氣化區域中跑出之熱還原氣體混合；較 佳地係藉由混合入已從C〇2純化之還原氣體中並以冷卻 狀態再循環。 調整流化床還原區域之溫度的另,一選擇權係應基於此 一事實，即預還原階段係加在至少一個關於含氧化鐵物質 之預加熱階段的後面，而且從預還原階段出來之反應過的 還原氣體（較佳地係在使一部份反應過的還原氣體分開後 )係用來預加熱該含氧化鐵物質。 經濟部中央標準局員工消費合作社印製 (讀先閱讀背面之注意事項再填寫本頁) 爲了使含氧化鐵物質之預加熱溫度調整至程序方法上 所需求，亦即使流化床還原區域之溫度調至最適當，用於 預加熱之反應過的還原氣體須適度地接受部份燃燒" 供實施該方法之設備包括至少兩個連續排列之流化床 反應器，其中含氧化鐵物質將以一個方向經由輸送導管從 流化床反應器通至流化床反應器，而還原氣體則經由還原 氣體連接導管以相反方向從流化床反應器通至流化床反應 器；此設備還包括一熔化器氣化器，彼可經由輸送導管以 含氧化鐵物質運轉的流動方向將來自排列最後之流化床反 本紙張尺度適用中國國家標準（CNS ) Λ4規格（210X297公釐） 一 Ί 一 A7 B7 五、發明説明（5 ) 應器的還原產物通入其內，同時彼涵蓋有含氧氣體與碳載 齊ί用之進料導管以及供生鐵或鋼預材料及礦渣用之螺栓， 和供熔化器氣化器中生成之還原氣體用的還原氣體進料導 管’此導管將以含氧化鐵物質之流動方向跑進排列在最後 之流化床反應器；其特徵爲一分枝導管係以含氧化鐵物質 之流動方向，從連接著排：^最後之流化床反應器與緊跟在 前之流化床反應器的還原氣體連接導管中分開，再經由滌 氣器、C〇2 -消去器具及氣體加熱器而跑入還原氣體進 料導管中。 較佳之具體實施例的特徵爲，該氣體加熱器可藉助於 一還原氣體旁道導管而迂迴通行。 在本文中，合適之還原氣體除灰器具備配有還原氣體 進料導管，而分枝導管係於還原氣體除灰器具與流化床反 應器之間的位置處跑進還原氣體進料導管內。 經濟部t央標隼局員工消費合作社印製 (請先閱讀背面之注意事項再填寫本頁) 另一較佳具體實施例之特徵爲，從還原氣體再循環導 管分開之還原氣體進料導管將經由滌氣器及壓縮器，並在 分開的氣體再循環導管前位位置處（以氣體流動方向來看 時），特別地係於安排在還原氣體進料導管內的除灰器具_ 前面位置處再返回進入該還原氣體進料導管內。 較有利地，從含氧化鐵物質之流動方向觀看時，第一 個流化床還原反應器係放在至少一個還原氣體卸料導管可 導入之預加熱反應器後面，此卸料導管是從第一個流化床 還原反應器（從含氧化鐵物質的流動方向觀之）離開；而 且，其中，一送進含氧氣體或氧氣之導管乃適於通入流化 張尺度適中國國家標準（CNS )人4^見格（21〇ίΪ97公釐） ： _ 8 _ A7 ___B7_ 五、發明説明（6 ) 床預加熱反應器內。 (請先閱讀背面之注意事項再填寫本頁) 本發明頃刻將以兩個如隨附之圖所解說的例證具體實 施例而更詳細地說明，每一圖1及圖2係以概括圖之形式 描述如本發明方法的有利變異。 根據本發明之設備提供有3個連續排列之流化床反應 器1至3，其中含氧化鐵，質如細礦是經由礦石供應導管 • 4送到第一個流化床反應器1中，其內在預加熱階段5中 可進行細礦之預加熱及視需要之預還原反應，隨後再經由 輸送導管6從流化床反應器1通到流化床反應器2，3中 。預還原反應係在流化床反應器2的預還原階段7中進行 ’而細礦變成海綿鐵之最後還原反應係於流化床反應器3 之最終還原階段8中操作。 、 經由輸送導管9 ，該完全還原之物質（即海綿鐵）將 經濟部尹央標準局員工消費合作社印製 導入熔化器氣化器1 0內。在熔化器氣化器1 〇內之熔化 氣化區域1 1中，含C0 -及Η2—之還原氣體係從煤及 含氧氣體中生成，再以細礦流動方向經由還原氣體進料導 管1 2導入排在最後的流化床反應器3中。此還原氣體隨 後將以細礦流動的逆流方向經由連接導管13從流化床反 應器3中通入流化床反應器2至1內，再以頂端氣體經由 頂端氣體卸料導管1 4從流化床反應器1中卸出，隨後則 於濕式滌氣器1 5中冷卻並洗滌。 熔化器氧化器1〇裝備有供固態碳載劑用之進料導管 1 6、供含氧氣體用之進料導管1 7、以及視需要之供碳 載劑’如烴類（室溫下爲液態或氣態）及煅燒之助熔劑用 本紙張尺度適用中國國家標隼（CNS ) Α4規格（210Χ297公釐） A7 B7 經濟部中央標準局員工消費合作社印製 器10中熔融生鐵或熔融之鋼 氣化區域1 1下面收集，其可 離開而通入流化床反應器3之 則提供有一除灰器具1 9，例 分離之灰粒子係經由以氮氣做 0、及經由一在氧氣注射下之 化器1 0中。 則將流化床反應器3與流化床 出一分枝導管2 1，一部份在 還原氣體將經由分枝導管21 係通入滌氣器2 2，再經由壓 〇 2 —消去器具2 4。舉例之 擺動式吸附裝置或C ◦ 2 ，滌 〇2消去器具2 4導;入氣體加 .原氣體進料導管1 2-內，而較 19與流化床反應器3之間的 床反應器3中反應過之還原氣 變得可行，隨後再加熱還原氣 的溫度，如此該氣體就可再次 氣體。因此，最終還原階段8 體，儘管最終還原階段8內有 當多量可用的還原劑也就不會 五、發明説明（7 ) 的進料導管。在熔化器#化 預材料及熔融礦渣係在熔化 經由螺栓1 8而放液。 在從熔化器氧化器1 0 還原氣體進料導管12中， 如熱分塵器，在該分塵器中 爲輸送介質之再循環導管2 燃燒器3 3而送入熔化器氧 還原氣體連接導管13 反應器2連接起來，但分岐 流化床反應器3中反應過的 而被帶走。此分枝導管2 1 縮器2 3而從滌氣器導向C ，此消去器具可設計成壓力 氣器。分枝導管21再從C 熱器25中，最後就通入還 佳地係通入在熱氣體分麈器 導管1 2內。 藉此，使一部份在流化 體除去C〇2達最大程度將 體至8 6 0與9 0 0 °C之間 地做爲具高還原電位之還原 將供應有特別多量的還原氣 相當高的溫度，但由於有相 本紙張尺度適用中國國家標準（CNS ) A4規格（210X297公釐） (請先閔讀背面之注意事項再填寫本頁) 訂 10 A7 ____B7_ 五、發明説明（8 ) 有"黏著〃之危險。 (讀先閱讀背面之注意事項再填寫本頁) 加熱一部份經由分枝導管21所帶走的還原氣體係以 再生或重複方式執行，或者是藉由部份燃燒此氣體而進行 ;其中這些加熱方法可單獨地或組合二或多個才應甩》 進行細礦之預還原反應的流化床反應器2裝備著更少· 量的還原氣體，這些還原_體展現較小的還原電位，但tf 預還原反應而言卻絕對足夠。由於此處該欲還原之物質要 達成的還原程度此最終還原階段8還低，所以就不會發生 "黏著"。因此，流化床反應器2及其氣體進料和卸料導 管1 3等係以通入此流化床反應器2內之還原氣體的還原 量爲函數來次元空間化。從此流化床反應器2出來之反應 過的還原氣體係經由導管1 3通入滌氣器2 6。一部份清 洗過且反應過之還原氣體則經由輸出氣體卸料導管2 7而 被抽出；另一部份便經由導管1 3通入預加熱階段5中， 亦即通入流化床反應器1。 經濟部中央標準局員工消費合作社印製 較佳地，氣體加熱器2 5可藉由旁道2 8而迂迴通行 一部份的再循環氣體，而旁道導管2 8係通入還原氣體進 料導管1 2，再連接著熔化器氧化器1 0與流化床反應器 3。因此，經由此旁道2 8，冷的再循環還原氣體可與從 熔化器氧化器1 0出來之熱還原氣體混合，體積控制可對 所需之還原氣體溫度做簡易的調節。 由於所提供之氣體再循環導管2 9可經由滌氣器3 0 及壓縮器3 1而離開還原氣體進料導管1 2，並再次地在 熱氣體分塵器19前面的位置處將一部份還原氣體回流到 本紙張尺度適用t國國家標準（CNS ) A4規格（210X29?公釐） 11 -11 一 A7 ____ B7 五、發明説明（9 ) 此還原氣體進料導管1 2內，因而可產生調整還原氣體溫 度的另一可行性。 根據圖1所述之方法變異或設備，在'每一流化床反應 器1至3後面都有一部份的反應過之還原氣體會被分開， 藉此，每一流化床反應器1至3僅送進能使备個流化床反 應器平順地作用所確實需考的氣體量。 根據圖2解說之方法變異，從流化床反應器2流出之 所有反應過的還原氣體將於預加熱階段5中使用，在此處 ，從流化床反應器2出來之反應過還原氣體的全部顯熱將 會用來預加熱細礦》 爲了調整細礦之預加熱溫度，可行的是將含氧氣體， 例如空氣或氧經由導管3 2供應至預加熱階段5 (亦即流 化床反應器1 )中，藉此就可進行該被送至預加熱階段5 之反應過還原氣體的部份燃燒作用。藉由控制部份燃燒作 用，便可調整預加熱操作期間之細礦溫度，如此即可使隨 後之還原階段7，8內的溫度臻至完善。 、 經濟部中央標隼局員工消費合作社印製 (請先閱讀背面之注意事項再填寫本頁) 本發明並不受限於圖中所解說之例證具障實施例，但 可以各種關聯來修正。舉例之，以選擇流化床反應器之數 目做爲實際需求的函數也是可行的。 實施例: 在相對應於圖1之設備中，將具有表I所示之化學組 成份的3 1 . 4 t煤/小時放入熔化器氧化器1 0中，以 便產生40t生鐵/小時，並用3 1 ，240Nm3 02 ^"氏張尺度適用中國國家標準（CNS ) A4規格（210X 297公釐） -12 - A7 B7 五、發明説明{ 1〇) / h氣化。 S_1_ 煤（乾燥） C 7 8 . 9 % Η 3 . 8 % Ν 1 . 0 % 〇 2 . 0 % 灰份 8 . 7 % C f i X 7 2 . 0 % (請先閱讀背面之注意事項再填寫本頁) 經濟部中央標準局員工消費合作社印製 將5 8. 6 t/h之量的礦石（具有如表II所示之礦 分析値）及8 . 6 t / h量之根據表III的助熔劑放入此設 備中。由·此設備所製造之生鐵展現了如表IV所述之化學組 成份。 ' 本紙張尺度適用中國國家標準（CNS ) A4規格（210X 297公釐）-13 - A7 B7 五、發明説明（11) 經濟部中央標準局員工消費合作社印製 表 II 表 III 表 IV 礦石 助熔劑 生鐵 (潮濕） Fe 64.9¾ CaO 45.0¾ C 4.2% Fe2〇3 92.4% MgO 9 % Si 0.3¾ LO I 0.3% S i 〇2 1 % Μη 0.04% 溫度 1 % A 1 2 0 3 0.5% Ρ 0 . 0 4 % 燒失量 40 % S 0.02% Fe 餘額 在熔化器氧化器1 0中， 還原氣體可產生6 3 . 4 4 N m 3/ h之量， 並具有8 7 0 °C之溫度。彼之化學組成 份乃示於表V中 。此還原氣體將與分枝導管 2 1所供應之 再循環還原氣體 (其量爲6 8 ，0 0 0 N m 3/ h， 且於 氣體加熱器2 5 中後加熱至8 7 0 °C之溫度 )混合， ，藉此 ，即可以1 1 6 .7 6 0 N m 3/h之量且溫度在8 7 0 °C的還原氣體供應到最終還原階段8中。此還原氣體具有 如表VI所示之化學組成份。 (请先閱讀背面之注意事項再填寫本頁) 本紙張尺度適用中國國家標準（CNS ) A4規格（210X 297公釐） 14 經濟部中央標準局員工消費合作社印製 A7 B7 五、發明説明（12) &——y~ s_π 來自熔化器氧化器1 0 之還原氣體 供用於最終還原階段 之還原氣體 C0 7 1 . 3 % * CO 6 2 . 2 % C〇2 0.6¾ C〇2 2.1% h2 23.0% h2 19.8¾ h2〇 0.5¾ h2〇 1 . 0% N 2 + A r 4.3% N 2 + A r 14.6¾ ch4 0 . 3% ch4 0.3% —部份其量約6 8，〇 〇 〇Nm3/h且具有表VII所 示之化學組成份的從最終還原階段8離逸之部份反應過還 原氣體將被抽回’再經由分枝導管2 1通入C 0，—滌氣 器2 4內。經由導管2 7及1 4所帶走之输出氣體有 4 7，7 2 ONm3/h的量。其化學組成份乃顯示於表 VIII ° (請先閲讀背面之注意事項再填寫本頁)Attachment 1: Amendment to the Chinese specification of Patent Application No. 85111751 for 10 households in the Republic of China in 1996. Forging is correct. 1-- V. Description of the invention (1) 〆 Continue to ask the commission to indicate whether the amended ^ is within the original substance ^ Printed by the Consumers' Cooperative of the Central Bureau of Standards, Ministry of Economics The present invention relates to a method for making molten pig iron or liquid steel pre-products from particulate matter containing iron oxide by fluidization, wherein the iron oxide-containing material is poor in In at least one pre-reduction stage, the rib is pre-reduced by a reducing gas, and then reduced to sponge iron in the final reduction stage. The sponge iron will be melted in the oxidation zone under the supply of carbon carrier and oxygen-containing gas. Melting, at the same time, a reduction gas containing C 0 — and H 2 — introduced into the final reduction stage and reacted there, then unloaded, and then introduced into the prereduction stage, should also be introduced into the prereduction stage. Will be reacted, unloaded, and then washed, and then taken away with the output gas; and at least a part of the reacted reducing gas can be purified, heated from CO2 and As for the use of recycled material reduction of iron oxide-containing reducing gas; apparatus for the implementation of the method of the present invention is also based. The method of this form can be known from US Patent No. A-5, 185, 032. When using this method, in order to achieve the maximum possible reduction potential and thermal energy of the reducing gas, the reducing gas will pass through all the reduction stages and through the pre-heating stage immediately preceding the flow direction of the iron oxide-containing material, and from It is withdrawn in the first pre-heating phase as the tip gas and subsequently cleaned. A portion of the top gas is compressed and subjected to CO2 elimination, followed by heating. The top gas, which is thus heated and purified from CO2 to a greater extent, is then sent to the reduction process as a recycled reducing gas, whereby the reducing agent still present in the top gas can be utilized. However, one of the disadvantages involved here is that each fluidized bed reduction stage and each pre-heating stage must be sized so that all the gases can be operated, that is, the newly produced reducing gas plus the recycled reducing gas . (Please read the precautions on the back page before ΛΜ page.) {Cns) A4W (210x297 ^). 4. &Quot; Attachment 1: Amendment to the Chinese Specification of Patent Application No. 85111751 for 10 households in 1996 -V. Explanation of the invention (1) 〆. Continue to ask the commissioner to indicate whether the revised version is within the original essence ^ Printed by the Consumers' Cooperative of the Central Bureau of Standards of the Ministry of Economic Affairs This invention is about Method for producing molten pig iron or liquid steel pre-product from micro-particles containing iron oxide, wherein the iron oxide-containing lean is pre-reduced by ribs in a reducing gas in at least one pre-reduction stage, and then in the final reduction stage It is reduced to sponge iron. Under the supply of carbon carrier and oxygen-containing gas, the sponge iron will be melted in the melting and oxidizing area, and at the same time, it can be produced. It is introduced into the final reduction stage and reacted, unloaded, and then introduced. The reducing gas containing C 0 — and H 2 — in the pre-reduction stage, similarly, the reducing gas introduced into the pre-reduction stage will also react, unload, and receive washing, and then be taken away with the output gas; and At least a part of the reacted reducing gas can be purified from CO2, heated 'and reused as a recycled reducing gas for the reduction of the iron oxide-containing substance; the present invention also relates to equipment for implementing the method. The method of this form can be known from US Patent No. A-5, 185, 032. When using this method, in order to achieve the maximum possible reduction potential and thermal energy of the reducing gas, the reducing gas will pass through all the reduction stages and through the pre-heating stage immediately preceding the flow direction of the iron oxide-containing material, and from It is withdrawn in the first pre-heating phase as the tip gas and subsequently cleaned. A portion of the top gas is compressed and subjected to CO2 elimination, followed by heating. The top gas, which is thus heated and purified from CO2 to a greater extent, is then sent to the reduction process as a recycled reducing gas, whereby the reducing agent still present in the top gas can be utilized. However, one of the disadvantages involved here is that each fluidized bed reduction stage and each pre-heating stage must be sized so that all the gases can be operated, that is, the newly produced reducing gas plus the recycled reducing gas . (Please read the precautions on the back page before ΛΜ page.) {Cns) A4W (210x297 ^). 4. &Quot; A7 B7 V. Description of the invention (2) Please read first-read the back, and then note the V " page In a reduction reaction using a C 0 / C 0 2 mixture and by fluidization of iron oxide, an increase in the reduction gas at high temperature (for example, more than 700 ° C) and at a lower reduction potential (that is, in the reducing gas) (: 〇2 and Η20 content) Oriented, needle-like iron precipitates exist on the surface of fine ore particles. In the fluidized bed, these iron precipitates begin to have a phenomenon of ^ adhesion. With very high During the reduction reaction, the agglomeration of the ore will occur, thus hindering the reduction process. However, if the reduction reaction is carried out at a very high or maximum reduction potential of the reducing gas, the iron precipitate will be dense or porous, No adhesion is observed in this way. The purpose of the present invention is to avoid these shortcomings and difficulties, and to provide a method and a device for implementing the method, which increase the reduction potential of the reducing gas to ensure the reduction reaction without * Adhesion 'happens, However, the amount of carbon carrier used to make the reducing gas has not increased: compared with the prior art, the carbon carrier can be saved instead. According to the present invention, only a part of the reduction from the final reduction stage to the pre-reduction stage is required. The gas can be separated, cleaned, purified from CO2, and 'heated', and then recycled to the final reduction stage. This can be achieved. Employees of the Central Bureau of Standards, Ministry of Economic Affairs, Consumer Consumption Du printed when using the method of the present invention It is correct to use the reduction potential that is still present in the reducing gas that comes out of the final reduction stage and is separated from the same reduction gas used for the other reduction stage and / or any pre-heating; from this fact it is possible to produce substantial Advantages: According to the present invention, a high reduction potential can be ensured by increasing the amount of reducing gas, wherein as the reduction process proceeds step by step, only an incremental amount of reducing gas needs to be provided in the final reduction stage. The temperature is the highest and the size of the sticky paper is applicable to the Chinese National Standard (CNS) A4 specification (210X 297 mm) A7 B7 V. Description of the invention (3) This means that "adhesion can be reliably avoided in the most dangerous final reduction stage", and the need to size all parts of the equipment (that is, all gas ducts, reactors, compressors, etc.) can be ruled out. Any pre-heating stage and fluidized-bed reduction stage provided by this method can be operated in incremental Liaoyuan gas. Therefore, the present invention can selectively utilize a high reduction potential, and as a result, other reduction stages can provide a theory The minimum amount of reducing gas, and the required equipment can be proportionally smaller, so it is less expensive. Inevitably, the present invention can not only size the parts of all equipment in the most appropriate way, that is, have the largest possible In production capacity, only the minimum amount of carbon carrier required to produce the reducing gas is used as far as possible; in other words, the coal consumption rate can be minimized, and at the same time any danger of sticking # can be reliably avoided. Furthermore, although coal can only form an insufficient amount of reducing gas, it will become feasible to use coal with high Cfix and low ash content in the melted gasification zone, and still achieve a uniform thermal equilibrium, that is, as long as the A small amount of water can be added to the melted gasification zone to increase the amount of reducing gas. Department of Economics, Central Bureau of Standards, Consumer Consumption Du printed V- (please M-read the precautions on the back) ^ # Since very high reduction potentials are applied in the final reduction stage, part of them are from the final reduction stage It should be taken out from the same gas and separated from the same gas, and then the reducing gas recycled to the same gas should be heated to a reduction temperature in the range of 800 to 900 ° C. For example, it can be heated to about 8 50 ° C . Advantageously, the reducing gas withdrawn and separated from the final reduction stage can be repeated and / or regenerated, and / or heated to the reducing temperature by partially burning the part of the withdrawn reducing gas. . Preferably, the recirculation of the heated reducing gas is performed by mixing the paper with the Chinese standard (CNS) A4 (210 X297 mm) _ 6-A7 B7 V. Description of the invention (4) The melting is performed in a hot reducing gas that has come out of the gasification zone and has been ashed. In order to cool the reducing gas leaving the dissolver gasifier to the reducing temperature, an appropriate part of the reducing gas purified from co2 will be recycled in a cooled state, preferably mixed into the reducing gas before they are introduced into the final reduction stage. In the melted gasification zone, escape from the hot reducing gas. Regarding the easy temperature adjustment in the final reduction stage, it is more advantageous to first clean a part of the hot reducing gas coming out of the melted gasification area, and then mix it with the hot reducing gas running out of the melted gasification area in a cooled state. ; Preferably by mixing into a reducing gas purified from CO 2 and recycling in a cooled state. Another option for adjusting the temperature in the reduction zone of the fluidized bed should be based on the fact that the pre-reduction stage is added after at least one pre-heating stage with respect to the iron oxide-containing substance, and the reaction from the pre-reduction stage The used reducing gas (preferably after separating a part of the reacted reducing gas) is used to preheat the iron oxide-containing substance. Printed by the Consumers' Cooperative of the Central Standards Bureau of the Ministry of Economic Affairs (Read the precautions on the back before filling this page) In order to adjust the preheating temperature of iron oxide-containing substances to the requirements of the program method, even the temperature of the fluidized bed reduction area Adjusted to the most appropriate, the reacted reducing gas used for preheating must moderately accept partial combustion "The equipment for carrying out the method includes at least two continuously arranged fluidized bed reactors, in which the iron oxide-containing material will be One direction passes from the fluidized bed reactor to the fluidized bed reactor via a conveying conduit, and the reducing gas passes from the fluidized bed reactor to the fluidized bed reactor in the opposite direction via the reducing gas connection conduit; the apparatus also includes a Melter vaporizer, which can flow through the conveying pipe to run in the direction of iron oxide containing material. The size of the paper from the last aligned fluidized bed is in accordance with the Chinese National Standard (CNS) Λ4 specification (210X297 mm). One A7 B7 V. Description of the invention (5) The reduction product of the reactor is passed into it, and at the same time, it covers the feed conduit for oxygen-containing gas and carbon, and the supply conduit Bolts for iron or steel pre-materials and slag, and a reducing gas feed conduit for reducing gas generated in the melter gasifier. This conduit will run in the direction of the flow of iron oxide-containing material and line up in the final fluidization. Bed reactor; characterized in that a branch duct is connected in a row from the direction of flow of iron oxide-containing material: ^ the last fluidized bed reactor and the reducing gas connection pipe immediately preceding the fluidized bed reactor It is then separated into a reducing gas feed duct through a scrubber, a CO2-elimination device and a gas heater. A preferred embodiment is characterized in that the gas heater can be bypassed by means of a reducing gas bypass duct. In this paper, a suitable reducing gas ash remover is provided with a reducing gas feed duct, and the branch duct runs into the reducing gas feed duct at a position between the reducing gas ash removing appliance and the fluidized bed reactor. . Printed by the Consumers ’Cooperative of the Central Bureau of Economic Affairs of the Ministry of Economic Affairs (please read the precautions on the back before filling this page) Another preferred embodiment is characterized in that the reducing gas feed duct separated from the reducing gas recirculation duct will be Pass the scrubber and compressor, and at the front position of the separate gas recirculation duct (as viewed from the direction of gas flow), especially tied to the ash removal device arranged in the reduction gas feed duct _ front position It then returns to the reducing gas feed conduit. Advantageously, when viewed from the flow direction of the iron oxide-containing material, the first fluidized-bed reduction reactor is placed behind a pre-heated reactor into which at least one reducing gas discharge duct can be introduced. A fluidized-bed reduction reactor (viewed from the direction of flow of the iron oxide-containing material) exits; and among them, a conduit for feeding oxygen-containing gas or oxygen is suitable for passing the fluidized sheet in accordance with Chinese national standards (CNS ) Person 4 ^ See grid (21〇ίΪ97mm): _ 8 _ A7 ___B7_ V. Description of the invention (6) The bed is preheated in the reactor. (Please read the notes on the back before filling this page) The present invention will be explained in more detail with two exemplified specific embodiments as illustrated in the accompanying drawings. Each of Figures 1 and 2 is a summary of the drawings. The form describes an advantageous variation of the method according to the invention. The device according to the invention is provided with three fluidized bed reactors 1 to 3 arranged in series, which contain iron oxides, such as fine ore, which are sent to the first fluidized bed reactor 1 via an ore supply duct, In the pre-heating stage 5, the pre-heating of fine ore and the pre-reduction reaction as needed can be carried out, and then the fluidized bed reactor 1 is passed to the fluidized bed reactors 2 and 3 through the conveying pipe 6. The prereduction reaction is performed in the prereduction stage 7 of the fluidized bed reactor 2 and the final reduction reaction of the fine ore to sponge iron is operated in the final reduction stage 8 of the fluidized bed reactor 3. Through the delivery duct 9, the completely reduced substance (ie sponge iron) is printed into the melter gasifier 10 by the Consumer Cooperative of Yinyang Standard Bureau of the Ministry of Economic Affairs. In the melter gasification zone 11 within the melter gasifier 10, a reducing gas system containing C0-and Η2-is generated from coal and oxygen-containing gas, and then flows through the reducing gas feed conduit 1 in the direction of fine ore flow. 2 is introduced into the last fluidized bed reactor 3. This reducing gas will then pass from the fluidized bed reactor 3 into the fluidized bed reactors 2 to 1 in the countercurrent direction of the flow of fine ore through the connecting pipe 13 and then flow from the flow through the top gas through the top gas discharge pipe 14 The fluidized bed reactor 1 is discharged and then cooled and washed in a wet scrubber 15. The melter oxidizer 10 is equipped with a feed conduit 16 for a solid carbon carrier, a feed conduit 17 for an oxygen-containing gas, and, if necessary, a carbon carrier 'such as hydrocarbons (at room temperature) Liquid or gaseous) and calcined fluxes. The paper size applies to Chinese National Standard (CNS) A4 specification (210 × 297 mm) A7 B7 Molten pig iron or molten steel gas in the printer 10 of the Consumer Cooperatives of the Central Standards Bureau of the Ministry of Economic Affairs Collected under the chemical zone 11, which can leave and pass into the fluidized bed reactor 3, a ash removal device 19 is provided. For example, the separated ash particles are made by nitrogen gas 0, and by chemical conversion under oxygen injection. Device 10. Then, the fluidized bed reactor 3 and the fluidized bed form a branch duct 21, and a part of the reducing gas will pass through the branch duct 21 to the scrubber 2 2 and then pass the pressure 02 to the elimination apparatus 2 4. For example, the swing type adsorption device or C 2, the elimination device 2 and the guide 2 2, the inlet gas and the original gas feed duct 1 2-, and the bed reactor between 19 and the fluidized bed reactor 3 The reacted reducing gas in 3 becomes feasible, and then the temperature of the reducing gas is heated again, so that the gas can be re-gased. Therefore, the final reduction stage 8 body, although there is a large amount of reducing agent available in the final reduction stage 8 will not be the feeding duct of the invention description (7). The preform and molten slag are melted in the melter, and the liquid is discharged through the bolt 18. In the feed pipe 12 for reducing gas from the melter oxidizer 10, such as a thermal duster, in this dust separator is a recirculation pipe 2 for conveying the medium. 13 Reactor 2 was connected, but the reaction in the divided fluidized bed reactor 3 was taken away. The branch duct 2 1 is retracted from the scrubber 2 3 and guided to C. The elimination device can be designed as a compressor. The branch pipe 21 is again passed from the C heater 25, and finally, the branch pipe 21 is preferably passed into the hot gas decanter pipe 12. In this way, a part of the fluidized body is removed from CO2 to a maximum extent. The body is reduced to a temperature between 860 and 900 ° C as a reduction with a high reduction potential, and a particularly large amount of reducing gas is supplied. High temperature, but due to the size of the paper, the Chinese National Standard (CNS) A4 specification (210X297 mm) is applied (please read the notes on the back before filling this page) Order 10 A7 ____B7_ V. Description of the invention (8) Yes " Danger of adhesion. (Read the precautions on the back before you fill out this page.) Heating part of the reducing gas system carried by the branching duct 21 is performed in a regenerative or repetitive manner, or by partially burning this gas; of these The heating method can be used alone or in combination of two or more. The fluidized bed reactor 2 for pre-reduction of fine ore is equipped with a smaller amount of reducing gas. These reducing bodies exhibit a smaller reduction potential. But tf pre-reduction is absolutely sufficient. Since the degree of reduction to be achieved by the substance to be reduced here is still low in this final reduction stage 8, " sticking " does not occur. Therefore, the fluidized bed reactor 2 and its gas feed and discharge conduits 13 and the like are dimensionally spaced as a function of the reduction amount of the reducing gas flowing into the fluidized bed reactor 2. The reacted reducing gas system exiting the fluidized-bed reactor 2 is passed to a scrubber 26 through a conduit 13. A part of the cleaned and reacted reducing gas is extracted through the output gas discharge duct 27; the other part is passed into the preheating stage 5 through the duct 13, that is, into the fluidized bed reactor 1. Printed by the Consumer Cooperative of the Central Standards Bureau of the Ministry of Economic Affairs. Preferably, the gas heater 25 can bypass a part of the recirculated gas through the bypass 28, and the bypass conduit 28 is connected to the reducing gas feed. The conduit 12 is further connected to the melter oxidizer 10 and the fluidized bed reactor 3. Therefore, through this bypass 28, the cold recirculated reducing gas can be mixed with the hot reducing gas from the melter oxidizer 10, and the volume control can easily adjust the required reducing gas temperature. Since the supplied gas recirculation duct 29 can pass through the scrubber 30 and the compressor 31, it can leave the reducing gas feed duct 12 and again a part of it at the position in front of the hot gas duster 19 The reducing gas is returned to the national standard (CNS) A4 specification (210X29? Mm) of this paper. 11 -11 A7 ____ B7 V. Description of the invention (9) The reducing gas feed pipe 12 can produce Another possibility to adjust the temperature of the reducing gas. According to the method variation or equipment described in FIG. 1, after each fluidized bed reactor 1 to 3, a part of the reacted reducing gas will be separated, whereby each fluidized bed reactor 1 to 3 Only feed in the amount of gas that really needs to be considered to make a fluidized bed reactor function smoothly. According to the variation of the method illustrated in FIG. 2, all the reacting reducing gas flowing out of the fluidized bed reactor 2 will be used in the preheating stage 5. Here, the reacting reducing gas coming out of the fluidized bed reactor 2 is All the sensible heat will be used to preheat the fine ore. In order to adjust the preheating temperature of the fine ore, it is feasible to supply an oxygen-containing gas, such as air or oxygen, to the preheating stage 5 through the conduit 32 (that is, the fluidized bed reaction). In the device 1), the partial combustion of the reacted reducing gas sent to the preheating stage 5 can be performed. By controlling part of the combustion effect, the fine ore temperature during the pre-heating operation can be adjusted, so that the temperature in the subsequent reduction stages 7, 8 can be perfected. Printed by the Consumer Cooperatives of the Central Bureau of Standards of the Ministry of Economic Affairs (please read the notes on the back before filling out this page) The present invention is not limited to the exemplified and impaired embodiments illustrated in the figure, but can be modified in various ways. For example, it is also feasible to select the number of fluidized bed reactors as a function of actual demand. Example: In an apparatus corresponding to FIG. 1, 3 1 .4 t coal / hour having the chemical composition shown in Table I is put into a melter oxidizer 10 so as to produce 40 t pig iron / hour, and used 3 1, 240Nm3 02 ^ " The Zhang scale is applicable to the Chinese National Standard (CNS) A4 specification (210X 297 mm) -12-A7 B7 V. Description of the invention {1〇) / h gasification. S_1_ Coal (dry) C 7 8.9% Η 3. 8% Ν 1. 0% 〇2. 0% Ash 8. 8% C fi X 7 2. 0% (Please read the notes on the back before filling (This page) The Consumer Cooperative of the Central Bureau of Standards of the Ministry of Economic Affairs prints the amount of 5 8. 6 t / h of ore (with ore analysis as shown in Table II) and the amount of 8. 6 t / h according to Table III. Flux is put into this device. Pig iron produced by this equipment exhibits chemical composition as described in Table IV. '' This paper size is in accordance with Chinese National Standard (CNS) A4 (210X 297mm) -13-A7 B7 V. Description of the invention (11) Printed by the Consumer Cooperatives of the Central Standards Bureau of the Ministry of Economy Table II Table III Table IV Ore Flux Pig iron (wet) Fe 64.9¾ CaO 45.0¾ C 4.2% Fe2〇3 92.4% MgO 9% Si 0.3¾ LO I 0.3% S i 〇2 1% Μη 0.04% Temperature 1% A 1 2 0 3 0.5% ρ 0. 0 4% Loss on ignition 40% S 0.02% Fe The balance is in the melter oxidizer 10, the reducing gas can produce an amount of 6 3.4. 4 N m 3 / h, and has a temperature of 870 ° C. Its chemical composition is shown in Table V. This reducing gas will be the same as the recirculating reducing gas supplied by the branch duct 21 (the amount is 6 8 0 0 0 N m 3 / h, and then heated to 8 7 0 ° C in the gas heater 2 5 Temperature), so that a reducing gas in an amount of 116.760 Nm3 / h and a temperature of 870 ° C can be supplied to the final reduction stage 8. This reducing gas has a chemical composition as shown in Table VI. (Please read the precautions on the back before filling this page) This paper size is applicable to the Chinese National Standard (CNS) A4 specification (210X 297 mm) 14 Printed by the Consumer Standards Cooperative of the Central Standards Bureau of the Ministry of Economic Affairs A7 B7 V. Description of the invention (12 ) & —— y ~ s_π The reducing gas from the melter oxidizer 10 is used for the reducing gas in the final reduction stage C0 7 1.3% * CO 6 2.2% CO2 0.6¾ CO2 2.1% h2 23.0% h2 19.8¾ h2〇0.5¾ h20.1. 0% N 2 + A r 4.3% N 2 + A r 14.6¾ ch4 0. 3% ch4 0.3%-part of the amount is about 68,000,000 Nm3 / h and has the chemical composition shown in Table VII, the part of the reaction reducing gas that escapes from the final reduction stage 8 will be pumped back 'and then through the branch duct 2 1 into C 0,-scrubber 2 4 Inside. The output gas taken through the conduits 27 and 14 has an amount of 47,7 2 ONm3 / h. Its chemical composition is shown in Table VIII ° (Please read the precautions on the back before filling this page)
本紙張尺度適用中國國家標準（CNS ) A4規格（210X 297公釐） 15 A7 B7 、發明説明（ 13) 表 VII 在 C 0 2 - -滌氣前面 分開之還原氣體，70°C CO 54.3% C〇2 1 1 . 8 % h2 16.8% h20 1 . 5% N 2 + A r 15.3% CH4 0.3%This paper size applies Chinese National Standard (CNS) A4 specification (210X 297 mm) 15 A7 B7, invention description (13) Table VII Reduction gas separated in front of C 0 2--scrubbing gas, 70 ° C CO 54.3% C 〇 2 1 1.8% h2 16.8% h20 1.5% N 2 + A r 15.3% CH4 0.3%
Μ_1LΜ_1L
輸出氣體，70°C !-------装-- - - t、 (請先閲讀背面之注意事項再填寫本頁) CO 39.9% C〇2 28.3% H2 13.2% H2O 1.6% N 2 + A r 16.7% ch4 0.3¾ 訂 經濟部中央標準局員工消費合作社印製 本紙張尺度適用中國國家標準（CNS ) A4規格（210 X 297公釐）-16Output gas, 70 ° C! ------- install ----t, (Please read the precautions on the back before filling this page) CO 39.9% C〇2 28.3% H2 13.2% H2O 1.6% N 2 + A r 16.7% ch4 0.3¾ Printed by the Consumers Cooperative of the Central Standards Bureau of the Ministry of Economic Affairs. The paper size is applicable to the Chinese National Standard (CNS) A4 (210 X 297 mm) -16