201033371 六、發明說明： 【發明所屬之技術領域】 本發明係有關於一種、用以在一熔煉區域中製造生鐵或 液態初級鋼製品之方法及裝置，其中含鐵礦爐料，及如果 適當，還有多種添加物在一還原區域中藉一還原氣體至少 部分地還原，然後被導引至該熔煉區域內，並連同被供入 之多種碳載體，尤其焦炭及/或煤，及含氧氣體一起被熔 @ 煉’從而形成還原氣體，其中該經形成之還原氣體被供應 至該還原區域，其在此處被轉化，且如果適當，在潔淨後 被當作輸出氣體抽出。 【先前技術】 由先前技藝可知，還原氣體的成分可調整。由美國第 3,909,244號專利可推知，處理來自天然氣重組器之還原氣 體以便可增加氫含量。然而，並未詳細地說明還原氣體之 利用。 ® 【發明內容】 因此，本發明之目的在於提供一種方法及裝置，其可 使熔煉還原程序更加地有效率，尤其是改良了還原氣體之 利用性》 此目的可藉由在申請專利範圍第1項中所請求之本發 明方法及在申請專利範圍第10項中所請求之本發明裝置 而達成。 藉由本發明之方法，輸出氣體中之至少一些將連同被 201033371 添加入之蒸氣及/或水在一轉化反應器中一起接受一氧化 碳轉化（CO轉化）。一經界定之氫（H2)對一氧化碳（CO) 的定量比被調定在輸出氣體中，且此還原氣體中之至少一 些被重新導引進入還原區域內及/或進入熔煉區域內作爲 經調修之還原氣體。此作法將使得該已在還原區域中用於 還原之經耗用的還原氣體可自此還原區域處被抽出。 從一鼓風爐或一還原爐腔處所抽出之還原氣體稱爲爐 頂氣，而從一流體化床反應器處所抽出者稱爲廢氣。這些 〇 名詞已經被歸納在集合名詞輸出氣體之下。此外，在熔煉 區域中之壓力調整可能產生一種所謂之過量氣體，其同樣 地被抽出並可連同輸出氣體一起被利用。來自熔煉單元之 還原氣體已可連同輸出氣體一起被利用。 轉化在一後續之處理中發生在一轉化反應器內，其中 在一連同添加入之蒸氣及/或水且藉由催化劑所進行之所 謂一氧化碳（CO)轉化中調定一氧化碳（CO )對氫（h2) Q 之比例。在此，可調整還原氣體，使其可被再導引至還原 區域內及/或熔煉區域內，並再度被利用於還原或當作一能 量載體。在此有利地，還原氣體在還原程序中之利用性將 可被改善，俾可減少在熔煉區域中用於產生還原氣體之碳 載體的數量。首先，富氧氣體之相當低密度意謂在還原區 域及/或熔煉區域中可有較小之液壓負荷。此也意謂可用預 先界定之設備大小達到更大之生產量，或者意謂可用一較 小之設備而達到一預先界定之生產能力。其次，由於還原 201033371 動力學特性將導致許多優點，此乃因爲氧化鐵成份 (Fe203、Fe304、FeO等）與氫（H2)之化學反應將顯著 地較與一氧化碳（CO)之反應更快。 當經調整之還原氣體被送回，其將與來自熔煉區域處 之還原氣體相混合，且因此可更有效率地調定此還原氣體 之成份。在此處，此經調整之還原氣體的直接送回很有利。 相較於輸入另一還原單元中，將富氧還原氣體送回至還原 區域內及/或熔煉區域內之優點在於：富氧氣體之經改善的 ❹ 還原動力學特性已經可被利用以在熔煉區域或還原區域中 增加產量。此外，並非絕對必需操作一個分離之還原單元 來產生直接之還原鐵，而此將使得可因爲省去此包括多個 附屬組件（洗滌器、水系統等）之類似還原爐腔而降低投 資成本。 根據本發明排出之方法的一有利改良型式，輸出氣體 在一氧化碳（CO)轉化前先被冷卻及潔淨，尤其是除麈及 Φ /或壓縮及/或再加熱，特別是利用來自經調整之還原氣體 的廢氣，已便可調定此一氧化碳（C0)轉化之處理溫度。 有利地，此一氧化碳（C0 )轉化僅使用經潔淨之輸出氣體’ 因爲此包含顯著比例之固體（例如灰塵）。在一些潔淨程序 (例如濕式潔淨程序之情形中，有必要首先冷卻此熱的輸 出氣體。如果必要，此經潔淨之輸出氣體將接著被再加熱 至一氧化碳（C0 )轉化所需之溫度。此再加熱可尤其有利 地運用來自該經調整之還原氣體的廢氣予以實現’因爲# 201033371 熱在一氧化碳（CO )轉化期間將被釋放。 根據本發明，輸出氣體當熱的時候在一氧化碳（C0 ) 轉化前被潔淨，尤其是在乾的時候被除塵，及/或被冷卻或 加熱’以便可調定此一氧化碳（CO )轉化之溫度。熱潔淨 程序使得再加熱實質上並不需要或將減少其進行期間所需 之能量。在特別熱之輸出氣體的情形中，甚至可完全免除 再加熱，或調定一供一氧化碳（CO)轉化過程中僅甩於冷 ^ 卻所需之溫度。 〇 根據本發明排出之方法的一特別有利改良型式，此經 調整之輸出氣體在被導引至還原區域及/或熔煉區域內之 刖先冷卻，且分離係藉由一分離方法（尤其是一吸附或吸 收方法）進行，其中二氧化碳（co2)至少部分地從該經條 修之還原氣體處被分離，並被當作爲尾氣去除。在二氧化 碳（C〇2)分離程序進行前之冷卻意謂顯著比例之蒸氣凝結 或分離出。 〇 來自二氧化碳（C02)分離程序之富二氧化碳（c〇2) 蒸氣被當作尾氣去除。二氧化碳（C02)與蒸氣必須去除， 因爲還原電位會被此二氧化碳（c〇2)與蒸氣降低。吸附或 吸收方法已證實在此有利，且同時經分離之二氧化碳（C02) 被當作所謂之尾氣而去除。這可被繼續傳遞以便進行隔離 或做進一步之處理，或者在使用吸附方法之情形中可排放 至大氣中。 諸如在生鐵製造設備中的真空壓力變動設備與壓力變 201033371 動設備之吸附方法已經因爲其低運轉成本而被證實是適宜 的。於這些設備中’在氫/一氧化碳（H2/C02 )之比例上的 增加將伴同在生產氣體產量上之增加，此乃因爲氫（H2) 的吸附力遠小於一氧化碳（C02 )與氮（n2)之吸附力，且 因此可達成較高之氫（H2)產量。氫（h2)之性質使得尤 其可以分離氫（h2)與氮（n2)，並因此可從回收氣體流處 將氮（n2 )驅逐出。 I 根據本發明排出之方法的一特別改良型式，經調整之 〇 還原氣體中之至少一些，尤其在二氧化碳（co2)與水（h2o) 自此經調整之還原氣體中被分離出後，與來自熔煉區域之 還原氣體相混合，且尤其在其已除塵之後，被供應至此還 原區域。藉由與來自熔煉區域之還原氣體間的相混合，可 調定或改造被導引至還原區域內之氣體混合物的成份與溫 度兩者。 根據本發明排出之方法的一特別改良型式’經調整之 Φ 還原氣體中之至少一些，尤其在二氧化碳（C02)與水（h20) 自此經調整之還原氣體中被分離出之後被加熱’如果適 當，則與來自熔煉區域處之已除塵的還原氣體相混合’並 被供應至此還原區域。額外之加熱將可將較大量之經調整 的還原氣體導引至還原區域內，尤其可調定諸還原狀況所 需要之高氣體溫度。此外，在氫/一氧化碳（H2/co)之比 例上的增加將可使此還原氣體被顯著地加熱於一間接熱交 換器中，因爲金屬塵化腐蝕可藉由高氫（H2)含量而被避 201033371 免，尤其是被添加在熱交換器之上游處的硫化氫（H2s)或 其他硫化合物。 根據本發明排出之方法的一適當改良型式，經調整之 還原氣體中之至少一些，如果適當，則在潔淨後與輸出氣 體相混合，並被供應至轉化反應器。在此，可調整整個氣 體混合物的成份而非只是輸出氣體的成份，且此使得可調 定一具有高還原程度之經調整還原氣體。此外，此還原氣 體之密度因爲此氣體與富氧氣體之相混合而減小，而此富 ❹ 氧氣體則係藉由一氧化碳（CO )轉化及水（h2o )與二氧 化碳（co2)之去除而產生。 此使得在相同差壓下可經由還原單元而供應更多之還 原氣體，且因此可達到直接還原鐵之增大生產成果或金屬 化。此外，氫/ 一氧化碳（h2/co )比例之調定將得以控制 還原反應器中之溫度管理，因爲經由一氧化碳（CO)所進 行之氧化鐵的還原主要爲放熱的，而經由氫（H2)者則主 Q 要爲吸熱的。 根據本發明排出之方法的一有利改良型式，在熔煉區 域中所產生之還原氣體中有一些，如果適當，則在潔淨後， 及如果適當，則在與輸出氣體及/或尾氣相混合後，被當作 一可燃氣體混合物從本方法中去除。不再被供應至還原區 域處之過量氣體被提供當作可用於其他用途之可燃燒氣體 混合物，其能含量尤其可經由燃燒而被利用。在最初先儲 存此諸氣體並平衡其成份係爲有利的，因爲尤其是尾氣具 201033371 有一很大變動之成份。 根據本發明，輸出氣體中有一些被供應至一膨脹渦輪 機，以便利用此輸出氣體之壓縮能。此膨賬渦輪機可改善 本方法之整體能量平衡。 根據本發明排出之裝置所提供者，來自一還原單元處 之輸出氣體中的至少一些可藉由一輸出氣體管線供至一轉 化反應器，以便進行一氧化碳（CO)轉化。此一氧化碳（CO) 轉化。此一氧化碳（CO)轉化涉及將輸出氣體連同被添加 入之蒸氣及/或水一起處理，其中一經界定之氫（H2)對一 氧化碳（CO)的定量比被調定在此輸出氣體中。此輸出氣 體可經由一供應管線而被當作經調整之還原氣體地導引至 還原單元內及/或至熔煉單元內。此經調整之還原氣體之返 回將可減少對可供在熔煉單元中生產還原氣體用之碳載體 的需求。此外，此設備之諸零件可被保持成小巧型態，亦 減少輸出氣體的量，以使可供處理經由本方法所逐出之輸 Q 出氣體用之裝置同樣地可較爲便宜。 根據本發明所實施之裝置的一可替代改良型式，輸出 氣體管線配備有一壓縮機，尤其一單級或多級式壓縮機， 及/或一輸入裝置，其用於吹動蒸氣及/或用於將水注入此 輸出氣體內。此壓縮機將可調定將還原氣體注射至處理反 應器內或至供給處理氣體管線內所需要之壓力。一氧化碳 (CO)轉化用之蒸氣及/或水可經由輸入裝置而被導引至輸 出氣體內。 -10- 201033371 根據本發明所實施之裝置的一可能變化型式所提供 者，輸出氣體管線配備有一可供冷卻用之冷卻裝置，尤其 一熱交換器，及/或一可供在一氧化碳轉化進行前先潔淨輸 出氣體用之潔淨裝置，尤其一濕式潔淨手段。此輸出氣體 最初由於連同輸出氣體穿過還原單元之微細顆粒狀固體與 灰塵而必須被潔淨。濕式潔淨方法之優點在於此諸固體與 灰塵能被可靠地分離。如果適當，此潔淨裝置之前可利用 一熱交換器進型冷卻，藉而可利用因此而在本方法中被去 ❹ 除之能量。 根據本發明之裝置的一可替代改良型式，輸出氣體管 線配備有一用於加熱此輸出氣體之熱交換器，如果適當， 則利用來自該經調整之還原氣體處的廢氣，及/或一輸入裝 置，其用於吹動蒸氣及/或用於將水注入輸出氣體內。此熱 交換器將可調定用於一氧化碳（CO)轉化所需之溫度。此 外，有效之加熱可藉由使用加熱用之熱的且經調整的還原 Q 氣體而達成。 根據本發明所實施之裝置的另一改良型式，輸出氣體 管線配備有一可供在一氧化碳轉化進行前先潔淨該熱的輸 出氣體用之乾式除塵手段。一乾式除塵手段（例如一熱氣 過濾器）之應用意謂此輸出氣體在除塵之前僅需被略微冷 卻，或甚至完全不需被冷卻。此將使得可將此輸出氣體之 能含量用於後續之一氧化碳（CO)轉化，且花費甚鉅之加 熱裝置因此可被省掉。 -11- 201033371 根據本發明所實施之裝置的一有利改良型式，還原氣 體管線配備有一或多個冷卻器，其用於冷卻該經調整之還 原氣體，用於冷凝及排出蒸氣。 此將可調定已在轉化反應器中被處理之氣體的壓力以 供後續步驟之用，並可排出來自經調整之還原氣體處之蒸 氣。此亦適用於該氣體之溫度，其可對應地降低。此對於 傳統之二氧化碳（.co2)分離方法（例如基於吸附或吸收原 理而進行之方法）而言係必須的，且因此只有在低進入溫 度下才運轉操作。 根據本發明所實施之裝置的一特別改良型式，設置一 從還原氣體管線處導引至一由熔煉單元引出之發電機氣體 管線處之冷卻氣體管線，使得該經調整之輸出氣體中之至 少一部分量可與來自熔煉單元且被供應至一尤其是旋風分 離器之除塵裝置處之還原氣體相混合。此經調整之輸出氣 體可進一步連同來自熔煉處之還原氣體一起被處理，亦即 Φ 被除麈並供給至該除塵單元處，以便可獲得一實質上均勻 之混合物，其具有大部分恆定之還原氣體成份。 根據本發明所實施之裝置的一特別有利改良型式，還 原單元構成爲鼓風爐之爐腔，或還原爐腔，或流體化床反 應器。諸如這些之單元已證實有利於藉還原氣體還原含鐵 礦之爐料。 根據本發明所實施之裝置的另一有利改良型式，熔煉 單元構成爲鼓風爐之下部，或熔爐氣化器。此熔煉單元在 -12- 201033371 此執行兩項工作：特定地熔煉經預先還原之含鐵爐料，以 及氣化碳載體並同時形成還原氣體。 根據本發明所實施之裝置的一特別改良型式，發電機 氣體管線進入還原氣體管線，使得來自熔煉單元之經調整 的輸出氣體及/或還原氣體可被導引至此還原單元內。此尤 其與來自熔煉單元處之已除塵的還原氣體間之混合將可影 響被供至此還原單元內之還原氣體的成份，且因此可確保 此還原氣體有一足夠之還原電位。 根據本發明所實施之裝置的一有利改良型式，設置一 從發電機氣體管線處導引至輸出氣體管線處之過量氣體管 線’其中過量氣體管線配備有一用於精細除塵之潔淨裝 置’尤其一濕式潔淨手段。此濕式潔淨手段可使還原氣體 連同亦已被有利地潔淨之輸出氣體一起被供給至轉化反應 器。此還原氣體與此輸出氣體之混合，如果適當，亦可連 同來自二氧化碳（C〇2)分離裝置處之尾氣—起，經由本方 Q 法去除，並例如繼續傳送以供熱應用。 根據本發明所實施之裝置的一可能變化型式，輸出氣 體去除管線配備有一膨脹渦輪機’以便可利用此輸出氣體 之壓縮能。此還原氣體之壓縮能可經由膨脹渦輪機而被利 用，並可用以產生能量。 下文中將經由範例並參照第1至4圖之附圖而更詳細 地敘述本發明。 【實施方式】 -13- 201033371 第1圖顯示根據本發明排出之裝置。含鐵礦之爐料ES 及添加物ZS在一當作一還原區域1之鼓風爐的爐腔中藉一 還原氣體至少部分地還原，接著被導引至熔煉區域2內， 亦即進入此鼓風爐之下部內，並熔煉以形成生鐵或初級鋼 製品。多種碳載體之氣化形成還原氣體，其在還原區域中 進行還原之後，作爲一輸出氣體而經由一輸出氣體管線4a 抽出，並首先在一乾式除麈手段21中預先潔淨，然後在一 _ 濕式潔淨器22中進一步潔淨。輸出氣體接著藉一壓縮機7201033371 VI. Description of the Invention: [Technical Field of the Invention] The present invention relates to a method and apparatus for producing pig iron or liquid primary steel products in a smelting zone, wherein the iron ore charge is, and if appropriate, A plurality of additives are at least partially reduced in a reduction zone by a reducing gas and then directed into the smelting zone, together with a plurality of carbon carriers, in particular coke and/or coal, and oxygen-containing gas being supplied It is fused to form a reducing gas, wherein the formed reducing gas is supplied to the reducing zone where it is converted and, if appropriate, extracted as an output gas after cleansing. [Prior Art] As is known from the prior art, the composition of the reducing gas can be adjusted. It is inferred from U.S. Patent No. 3,909,244 to treat a reducing gas from a natural gas recombiner so as to increase the hydrogen content. However, the use of reducing gas has not been explained in detail. SUMMARY OF THE INVENTION Accordingly, it is an object of the present invention to provide a method and apparatus that can make a smelting reduction process more efficient, and in particular, improve the utilization of a reducing gas. The method of the present invention as claimed in the item and the apparatus of the present invention as claimed in claim 10 of the patent application are achieved. By the method of the present invention, at least some of the output gas will undergo carbon monoxide conversion (CO conversion) together with the steam and/or water added by 201033371 in a conversion reactor. A defined ratio of hydrogen (H2) to carbon monoxide (CO) is set in the output gas, and at least some of the reducing gas is redirected into the reduction zone and/or into the smelting zone as a modified Reduced gas. This practice will allow the spent reducing gas that has been used for reduction in the reduction zone to be withdrawn therefrom. The reducing gas extracted from a blast furnace or a reducing furnace chamber is referred to as a top gas, and the extract from a fluidized bed reactor is referred to as an exhaust gas. These 〇 nouns have been summarized under the collective noun output gas. Furthermore, the pressure adjustment in the smelting zone may produce a so-called excess gas which is likewise withdrawn and which can be utilized together with the output gas. The reducing gas from the smelting unit can already be utilized along with the output gas. The conversion takes place in a subsequent reaction in a conversion reactor in which carbon monoxide (CO) is hydrogenated in a so-called carbon monoxide (CO) conversion carried out by addition of steam and/or water by means of a catalyst ( H2) The ratio of Q. Here, the reducing gas can be adjusted so that it can be redirected into the reduction zone and/or within the smelting zone and reused for reduction or as an energy carrier. Advantageously, the availability of the reducing gas in the reduction process can be improved, and the amount of carbon carrier used to generate the reducing gas in the smelting zone can be reduced. First, the relatively low density of oxygen-enriched gas means that there is less hydraulic loading in the reduction zone and/or the smelting zone. This also means that a larger production capacity can be achieved with a pre-defined device size, or that a pre-defined production capacity can be achieved with a smaller device. Secondly, the reduction of the kinetics of 201033371 will lead to many advantages, since the chemical reaction of iron oxide components (Fe203, Fe304, FeO, etc.) with hydrogen (H2) will be significantly faster than the reaction with carbon monoxide (CO). When the adjusted reducing gas is sent back, it will mix with the reducing gas from the smelting zone, and thus the composition of the reducing gas can be more efficiently set. Here, the direct return of this adjusted reducing gas is advantageous. An advantage of returning the oxygen-rich reducing gas to the reduction zone and/or the smelting zone as compared to the input of another reduction unit is that the improved enthalpy reduction kinetics of the oxygen-rich gas can already be utilized for smelting Increase production in the area or reduction area. Furthermore, it is not absolutely necessary to operate a separate reduction unit to produce direct reduced iron, which would make it possible to reduce capital costs by eliminating the need for a similar reduction furnace chamber comprising a plurality of accessory components (scrubber, water system, etc.). According to an advantageous further development of the method according to the invention, the output gas is cooled and cleaned prior to the conversion of carbon monoxide (CO), in particular by enthalpy and Φ/or compression and/or reheating, in particular from an adjusted reduction. The exhaust gas of the gas can be set to the treatment temperature of this carbon monoxide (C0) conversion. Advantageously, this carbon monoxide (C0) conversion uses only a cleaned output gas 'because this contains a significant proportion of solids (e.g., dust). In some cleansing procedures (such as wet cleaning procedures, it is necessary to first cool the hot output gas. If necessary, the cleaned output gas will then be reheated to the temperature required for carbon monoxide (C0) conversion. Reheating can be particularly advantageously carried out using exhaust gas from the conditioned reducing gas 'because #201033371 heat will be released during carbon monoxide (CO) conversion. According to the invention, the output gas is converted to carbon monoxide (CO) when hot The front is cleaned, especially when dry, and/or cooled or heated to adjust the temperature of this carbon monoxide (CO) conversion. The thermal cleansing procedure makes reheating substantially unnecessary or will reduce it. The energy required during the period. In the case of a particularly hot output gas, it is even possible to completely dispense with reheating, or to set a temperature required for the carbon monoxide (CO) conversion process to be only cold. A particularly advantageous refinement of the method of discharging, the adjusted output gas being directed into the reduction zone and/or the smelting zone Cooling first, and the separation is carried out by a separation method (especially an adsorption or absorption method) in which carbon dioxide (co2) is at least partially separated from the stripped reducing gas and removed as off-gas. C〇2) Cooling before the separation process means that a significant proportion of the vapor is condensed or separated. 富 Carbon dioxide-rich (c〇2) vapor from the carbon dioxide (C02) separation process is removed as tail gas. Carbon dioxide (C02) and vapour It must be removed because the reduction potential is reduced by this carbon dioxide (c〇2) and vapor. Adsorption or absorption methods have proven to be advantageous here, and at the same time the separated carbon dioxide (C02) is removed as so-called tail gas. Continue to pass for isolation or further processing, or to vent to the atmosphere in the case of adsorption methods. Vacuum pressure fluctuation equipment such as in pig iron manufacturing equipment and pressure change 201033371 The adsorption method of the mobile equipment has been operated because of its low operation. The cost has proven to be appropriate. In these devices, the ratio of hydrogen to carbon monoxide (H2/C02) The increase in the case will be accompanied by an increase in the production gas production, because the adsorption of hydrogen (H2) is much smaller than the adsorption of carbon monoxide (C02) and nitrogen (n2), and thus higher hydrogen (H2) can be achieved. Yield. The nature of hydrogen (h2) makes it possible, in particular, to separate hydrogen (h2) from nitrogen (n2) and thus to expel nitrogen (n2) from the recycle gas stream. I A particularly improved version of the process according to the invention. Adjusting at least some of the reducing gas, especially after the carbon dioxide (co2) and water (h2o) are separated from the adjusted reducing gas, mixed with the reducing gas from the smelting zone, and especially After being dedusted, it is supplied to the reduction zone. By mixing with the reducing gas from the smelting zone, both the composition and the temperature of the gas mixture introduced into the reduction zone can be tuned or modified. A particularly modified version of the method according to the invention, at least some of the adjusted Φ reducing gases, in particular after the carbon dioxide (C02) and water (h20) are separated from the adjusted reducing gas, are heated Suitably, it is mixed with the dedusted reducing gas from the smelting zone and supplied to this reducing zone. Additional heating will direct a relatively large amount of the adjusted reducing gas into the reduction zone, particularly the high gas temperatures required for the reduction conditions. In addition, an increase in the ratio of hydrogen/carbon monoxide (H2/co) will allow the reducing gas to be significantly heated in an indirect heat exchanger because metal dusting corrosion can be caused by high hydrogen (H2) content. Avoid 201033371 exemption, especially hydrogen sulfide (H2s) or other sulfur compounds added upstream of the heat exchanger. According to a suitable modification of the method of discharge of the present invention, at least some of the adjusted reducing gases, if appropriate, are mixed with the output gas after cleaning and supplied to the conversion reactor. Here, the composition of the entire gas mixture can be adjusted rather than just the component of the output gas, and this allows an adjusted reducing gas having a high degree of reduction to be adjusted. In addition, the density of the reducing gas is reduced by mixing the gas with the oxygen-rich gas, and the oxygen-rich gas is produced by carbon monoxide (CO) conversion and removal of water (h2o) and carbon dioxide (co2). . This allows more reducing gas to be supplied via the reduction unit at the same differential pressure, and thus an increase in production or metallization of direct reduced iron can be achieved. In addition, the hydrogen/carbon monoxide (h2/co) ratio setting will control the temperature management in the reduction reactor because the reduction of iron oxide via carbon monoxide (CO) is mainly exothermic, while those via hydrogen (H2) Then the main Q is to absorb heat. According to an advantageous further development of the method according to the invention, some of the reducing gases produced in the smelting zone, if appropriate, after cleaning, and if appropriate, after mixing with the output gas and/or the tail gas phase, It is removed from the process as a combustible gas mixture. Excess gas that is no longer supplied to the reduction zone is provided as a combustible gas mixture that can be used for other purposes, the energy content of which can be utilized, inter alia, by combustion. It is advantageous to store the gases and balance their composition at first, because in particular, the exhaust gas 201033371 has a very large variation. According to the present invention, some of the output gas is supplied to an expansion turbine to utilize the compression energy of the output gas. This swell turbine can improve the overall energy balance of the method. According to the apparatus of the present invention, at least some of the output gas from a reduction unit can be supplied to a conversion reactor through an output gas line for carbon monoxide (CO) conversion. This carbon monoxide (CO) conversion. This carbon monoxide (CO) conversion involves treating the output gas along with the added vapor and/or water, wherein a defined ratio of hydrogen (H2) to carbon monoxide (CO) is set in the output gas. This output gas can be directed into the reduction unit and/or into the smelting unit as a regulated reducing gas via a supply line. The return of this adjusted reducing gas will reduce the need for a carbon support for the production of reducing gases in the smelting unit. In addition, the components of the apparatus can be maintained in a compact form and also reduce the amount of output gas so that the means for treating the Q-out gas ejected by the method can be similarly inexpensive. According to an alternative refinement of the device according to the invention, the output gas line is provided with a compressor, in particular a single or multi-stage compressor, and/or an input device for blowing steam and/or Water is injected into the output gas. This compressor will be tuned to inject the reducing gas into the process reactor or to the pressure required to supply it into the process gas line. Vapor and/or water for carbon monoxide (CO) conversion can be directed into the output gas via an input device. -10-201033371 According to a possible variant of the device according to the invention, the output gas line is provided with a cooling device for cooling, in particular a heat exchanger, and/or one for carbon monoxide conversion before Clean the clean gas for the output gas first, especially a wet cleaning method. This output gas must initially be cleaned up by the fine particulate solids and dust that pass through the reduction unit along with the output gas. The advantage of the wet cleaning method is that the solids and dust can be reliably separated. If appropriate, the clean unit can be cooled by a heat exchanger prior to use, thereby utilizing the energy thus removed in the method. According to an alternative development of the device according to the invention, the output gas line is provided with a heat exchanger for heating the output gas, if appropriate, with exhaust gas from the adjusted reducing gas, and/or an input device It is used to blow steam and/or to inject water into the output gas. This heat exchanger will be tuned for the temperature required for carbon monoxide (CO) conversion. In addition, effective heating can be achieved by using a hot, adjusted, reduced Q gas for heating. According to another refinement of the apparatus embodying the invention, the output gas line is provided with a dry dust removal means for purifying the heat output gas prior to carbon monoxide conversion. The application of a dry dust removal means (e.g., a hot gas filter) means that the output gas only needs to be slightly cooled prior to dust removal, or even no need to be cooled at all. This will allow the energy content of this output gas to be used for subsequent carbon monoxide (CO) conversion, and the costly heating device can therefore be eliminated. -11- 201033371 An advantageous refinement of the apparatus according to the invention, the reducing gas line is provided with one or more coolers for cooling the conditioned reducing gas for condensing and venting the vapor. This will modulate the pressure of the gas that has been treated in the conversion reactor for subsequent steps and will vent the vapor from the conditioned reducing gas. This also applies to the temperature of the gas, which can be correspondingly reduced. This is necessary for conventional carbon dioxide (.co2) separation processes, such as those based on adsorption or absorption principles, and therefore operates only at low entry temperatures. According to a particular refinement of the apparatus according to the invention, a cooling gas line leading from the reducing gas line to a generator gas line drawn from the smelting unit is provided such that at least a portion of the conditioned output gas is provided The amount can be mixed with the reducing gas from the smelting unit and supplied to a dust removal device, in particular a cyclone. The conditioned output gas can be further processed along with the reducing gas from the smelting zone, i.e., Φ is removed and supplied to the dusting unit to obtain a substantially uniform mixture having a majority of constant reduction. Gas composition. According to a particularly advantageous refinement of the device according to the invention, the reducing unit is constructed as a furnace chamber of a blast furnace, or a reduction furnace chamber, or a fluidized bed reactor. Units such as these have proven to be advantageous for reducing the charge of iron-bearing ore by reducing gas. According to a further advantageous refinement of the device according to the invention, the smelting unit is formed as a lower part of the blast furnace or a furnace gasifier. This smelting unit performs two tasks at -12-201033371: specifically smelting the pre-reduced iron-containing charge, and vaporizing the carbon support and simultaneously forming a reducing gas. According to a particularly modified version of the apparatus embodied in the present invention, the generator gas line enters the reducing gas line such that the adjusted output gas and/or reducing gas from the smelting unit can be directed into the reduction unit. This mixing, in particular with the dedusted reducing gas from the smelting unit, will affect the composition of the reducing gas supplied to the reducing unit, and thus ensure that the reducing gas has a sufficient reduction potential. According to an advantageous further development of the device according to the invention, an excess gas line leading from the generator gas line to the output gas line is provided, wherein the excess gas line is provided with a cleaning device for fine dust removal, in particular a wet Clean means. This wet cleaning means allows the reducing gas to be supplied to the conversion reactor along with the output gas which has also been advantageously cleaned. The mixing of this reducing gas with this output gas, if appropriate, can also be carried out in conjunction with the off-gas from the carbon dioxide (C〇2) separation unit, via the Q method of the present, and, for example, continued to be transferred for heating applications. According to a possible variant of the device according to the invention, the output gas removal line is provided with an expansion turbine so that the compression energy of the output gas can be utilized. The compression energy of this reducing gas can be utilized via an expansion turbine and can be used to generate energy. The invention will be described in more detail hereinafter by way of example and with reference to the drawings of Figures 1 to 4. [Embodiment] -13- 201033371 Fig. 1 shows a device for discharging according to the present invention. The iron ore-containing charge ES and the additive ZS are at least partially reduced by a reducing gas in a furnace chamber of a blast furnace as a reduction zone 1, and then introduced into the smelting zone 2, that is, into the lower part of the blast furnace. Inside, and smelted to form pig iron or primary steel products. The gasification of a plurality of carbon carriers forms a reducing gas which, after reduction in the reduction zone, is withdrawn as an output gas via an output gas line 4a and is first pre-cleaned in a dry decanting means 21, then in a wet The cleaner 22 is further cleaned. The output gas is then borrowed from a compressor 7
G 壓縮，並在一熱交換器12中進一步加熱，且調定轉化反應 器5之過程溫度。蒸氣及/或水經由一輸入裝置8之添加會 導致一氧化碳（CO )轉化，而一氧化碳（CO )對氫（H2 ) 之比例被調定。 在此過程中所產生之二氧化碳（co2)及仍部分地存在 之水（H20)將藉由一熱交換器或藉由一冷凝器及一二氧化 碳（C02)分離裝置分離，並被當作尾氣TG，經由一尾氣 Q 管線23去除。此尾氣TG亦可隨意利用於加熱裝置20中 加熱經調整之還原氣體，而此尾氣至少部分地連同供入之 氣體及/或爐頂氣一起燃燒。加熱裝置20亦可成一熱交換 器之形式（例如氣體-氣體類型者）。 在轉化反應器5中處理之輸出氣體可在一熱交換器12 中之二氧化碳（C02)分離進行前先冷卻，而可在輸出氣體 被導引至轉化反應器5內之前先利用廢熱來加熱此輸出氣 體。在一氧化碳（CO)轉化進行之後，經調整之還原氣體 -14- 201033371 首先藉由冷卻器14冷卻。在二氧化碳（C02)分離進行之 後，此經調整之還原氣體被再導引至還原區域內。此可能 在鼓風爐之爐腔25中直接地或者經由伸入用於注射含氧 氣體（尤其含大於80%氧氣者）之噴管內之噴槍而發生。 在其被導引至還原區域內時，該經調整之還原氣體較佳地 應藉由加熱裝置20加熱。此加熱裝置可藉由將尾氣連同添 加入之空氣一起燃燒加熱。這在輸入（尤其注射入）鼓風 _ 爐之爐腔2 5內之情形中尤有必要。 〇 過量之輸出氣體亦可供至膨脹渦輪機19，以便可利用 此輸出氣體之壓縮能。此過量之輸出氣體及尾氣可被緩衝 儲存於一收集容器26中。在此，因爲該尾氣具有一會大幅 變動的成分，所以氣體混合物之成分也將平衡。 第2圖顯示本發明在一設備中之情形，而此設備具有 一熔煉單元2及四個流體化床反應器Rl、R2、R3及R4, 其以串聯方式連接，且其中爐料至少部分地還原。這些爐 Q 料在熱（HCI)時可被壓緊，並連同供入之煤塊SK或煤磚 BK，如果適當，結合注入煤粉，在熔煉單元中進一步處理 或在另一熔煉單元中部分地處理，以便增加性能或節省還 原劑。 針對從流體化床反應器R1處所抽出之輸出氣體的處 理，如果適當，包括在一熱交換器10中之冷卻以及在一潔 淨裝置11中之相關聯除塵，尤其是濕式潔淨。在藉由一壓 縮機所進行的壓縮及藉由一熱交換器12所進行的加熱之 -15- 201033371 後緊跟隨在轉化反應器5中所進行之一氧化碳（CO)轉化， 並同時經由一輸入裝置8而加入蒸氣及/或水。在分離二氧 化碳（co2)與水（H20 )後，一些經調整之還原氣體，尤 其是爲了冷卻之目的，而可與來自熔煉單元2處之還原氣 體相混合，並在除塵之後被供給至流體化床反應器R1或者 一供給容器27。經調整之還原氣體的溫度與還原氣體之溫 度亦可經由一可具有一潔淨裝置與一壓縮機之冷卻氣體管 線15而被影響。如果需要，此經調整之還原氣體亦可另外 ❹ 再藉由一加熱裝置20加熱。輸出氣體與來自熔煉單元2之 還原氣體的所構成之氣體混合物可被導引至輸出氣體管線 4b內，並因此供至該轉化反應器處。 來自二氧化碳（C02)分離裝置之尾氣TG或爐頂氣或 廢氣及/或過量氣體可經由連接管線13a、13b供至加熱裝 置20，這些氣體在此處被至少部分地燃燒，並因此可用於 加熱該經調整之還原氣體。過量之輸出氣體可經由一管線 φ 4c而供至一膨脹渦輪機19處，並在一收集容器26中均質 化。 第3及4圖顯示本發明在一設備中之情形，而此設備 則包括一熔煉單元2及一設計爲一還原爐腔之還原單元 1。礦石塊或顆粒在此還原單元1中被至少部分地還原，以 便形成直接還原鐵（HDRI )。此HDRI，如果適當，連同添 加入之緊壓還原鐵（CDRI )可在熔煉單元2中連同添加入 之煤K及微粒狀礦石FE被熔煉，以便形成生鐵PE。這些 -16- 201033371 圖式中本發明之諸特徵類似於第1及2圖中所示之實施例 實施》 【圖式簡單說明】 第1圖顯示一根據本發明而藉用一鼓風爐排出之改良 型式。 第2圖顯示一根據本發明而藉用一熔煉單亓 X及多個成 串聯連接的流體化床反應器排出之改良型式。 第3及4圖顯示一根據本發明而藉用一熔煉 〇 琛壌元及一 還原單元排出之改良型式。 【主要元件符號說明】 1 還原單元 2 熔煉單元 3 a/3 b 還原氣體管線 4/4a/4b/4c 輸出氣體管線 5 轉化反應器 6 a/-6 b 供給管線 7 壓縮機 8 蒸氣及/或水之輸入裝置 9 二氧化碳分離裝置 10 冷卻裝置 11 潔淨裝置 12 熱交換器 1 3a/l 3b 連接管線 -17- 201033371 14 冷 卻 器 15 冷 卻 器 體 管 線 16 旋 風 分 離 器 17 過 量 器 體 管 線 18 潔 淨 裝 置 19 膨 脹 渦 輪 機 20 加 熱 裝 置 2 1 乾 式 除 塵 手 段 22 濕 式 潔 淨 器 23 尾 氣 管 線 24 環 狀 氣 am 體 管 線 25 鼓 風 爐 之 爐 腔 26 收 集 容 器 27 供 給 容 器G is compressed and further heated in a heat exchanger 12 and the process temperature of the conversion reactor 5 is set. The addition of steam and/or water via an input device 8 results in the conversion of carbon monoxide (CO), which is set at a ratio of carbon monoxide (CO) to hydrogen (H2). The carbon dioxide (co2) produced during this process and the still partially present water (H20) will be separated by a heat exchanger or by a condenser and a carbon dioxide (C02) separation unit and used as tail gas TG. , removed via a tail gas Q line 23. The tail gas TG is also optionally utilized in the heating unit 20 to heat the adjusted reducing gas, and the tail gas is at least partially combusted together with the supplied gas and/or top gas. Heating device 20 can also be in the form of a heat exchanger (e.g., a gas-gas type). The output gas treated in the conversion reactor 5 can be cooled before the carbon dioxide (C02) in the heat exchanger 12 is separated, and the waste heat can be used to heat the output gas before being introduced into the conversion reactor 5. Output gas. After the carbon monoxide (CO) conversion is carried out, the adjusted reducing gas -14-201033371 is first cooled by the cooler 14. After the carbon dioxide (C02) separation is carried out, the adjusted reducing gas is redirected into the reduction zone. This may occur either in the furnace chamber 25 of the blast furnace or directly through a lance that is inserted into a nozzle for injecting an oxygen-containing gas, particularly one containing more than 80% oxygen. The adjusted reducing gas should preferably be heated by the heating means 20 as it is directed into the reduction zone. This heating device can be heated by burning off the exhaust gas together with the added air. This is especially necessary in the case of input (especially injection) into the furnace chamber 25 of the blast furnace.过量 Excess output gas is also available to the expansion turbine 19 so that the compression energy of the output gas can be utilized. The excess output gas and off-gas can be buffered and stored in a collection vessel 26. Here, since the exhaust gas has a component which greatly changes, the composition of the gas mixture will also be balanced. Figure 2 shows the situation of the present invention in an apparatus having a smelting unit 2 and four fluidized bed reactors R1, R2, R3 and R4 connected in series, and wherein the charge is at least partially reduced . These furnaces Q can be compacted during heat (HCI) and, together with the supplied coal block SK or briquettes BK, if appropriate, combined with injection of pulverized coal, further processed in the smelting unit or partially in another smelting unit Treatment to increase performance or save reductant. The treatment of the output gas withdrawn from the fluidized bed reactor R1, if appropriate, includes cooling in a heat exchanger 10 and associated dedusting in a cleaning device 11, especially wet cleaning. Following the compression by a compressor and the heating by a heat exchanger 12, -15-201033371, followed by a conversion of carbon monoxide (CO) in the conversion reactor 5, and simultaneously via an input Device 8 is added with steam and/or water. After separating carbon dioxide (co2) from water (H20), some of the adjusted reducing gas, especially for cooling purposes, can be mixed with the reducing gas from the smelting unit 2 and supplied to the fluidized after dust removal. Bed reactor R1 or a supply vessel 27. The temperature of the adjusted reducing gas and the temperature of the reducing gas can also be affected by a cooling gas line 15 which can have a clean unit and a compressor. If desired, the adjusted reducing gas may be additionally heated by a heating device 20. The resulting gas mixture of the output gas and the reducing gas from the smelting unit 2 can be directed into the output gas line 4b and thus supplied to the conversion reactor. Exhaust gas TG or top gas or exhaust gas and/or excess gas from the carbon dioxide (C02) separation unit can be supplied to the heating device 20 via connecting lines 13a, 13b, where they are at least partially combusted and thus can be used for heating The adjusted reducing gas. Excess output gas can be supplied to an expansion turbine 19 via a line φ 4c and homogenized in a collection vessel 26. Figures 3 and 4 show the situation of the present invention in a device which includes a melting unit 2 and a reduction unit 1 designed as a reduction furnace chamber. The ore block or granule is at least partially reduced in this reduction unit 1 to form direct reduced iron (HDRI). This HDRI, if appropriate, together with the addition of compacted reduced iron (CDRI), can be smelted in the smelting unit 2 together with the added coal K and particulate ore FE to form pig iron PE. The features of the present invention in the drawings are similar to those of the embodiments shown in Figures 1 and 2 [Simplified Description of the Drawings] Figure 1 shows an improvement of the use of a blast furnace in accordance with the present invention. Type. Figure 2 shows an improved version of a fluidized bed reactor with a smelting unit X and a plurality of series connected fluidized bed reactors in accordance with the present invention. Figures 3 and 4 show an improved version of a smelting unit and a reduction unit for discharge according to the present invention. [Main component symbol description] 1 Reduction unit 2 Melting unit 3 a/3 b Reduction gas line 4/4a/4b/4c Output gas line 5 Conversion reactor 6 a/-6 b Supply line 7 Compressor 8 Vapor and/or Water input device 9 Carbon dioxide separation device 10 Cooling device 11 Clean device 12 Heat exchanger 1 3a/l 3b Connecting line -17- 201033371 14 Cooler 15 Cooler body line 16 Cyclone separator 17 Excess body line 18 Clean unit 19 Expansion turbine 20 Heating device 2 1 Dry dust removal means 22 Wet cleaner 23 Exhaust line 24 Annular gas am line 25 Blast furnace chamber 26 Collection container 27 Supply container
-18--18-