200827452 九、發明說明： 【發明所屬之技術領域】 本發明係關於一種製造熔融金屬的方法，其中氧、還 原劑和在還原反應器中被還原的鐵係被引至炫融氣化爐 内，還原劑以氧所氣化，且還原的鐵以在此情況中出現的 熱來熔融，使用來自熔融氣化爐之熔鐵爐氣體作為至少一 部分的還原氣體，以及將經反應的爐頂氣從還原反應器中 移除；且本發明也關於一種執行該方法的工場，其具有還 原反應器、具有含有氧供給的熔融氣化爐，以及具有還原 劑的供應系統，至少一條绫政田忠^1 ^ ^愫琛路用來攸熔融氣化爐將熔鐵爐 氣體供應至還原反庫哭，日$ ,丨、 ^ ^ k原夂應抑且至少一條線路用來從還原反應 器中移除爐頂氣。 【先前技術】 t已在例如GB 883 998 A中所描述，在鼓風爐中，各 種含碳氣體，像是天然氣、煉焦爐氣等，係經由風口或在 爐腹平面中注入，目的在於節省焦煤和增加收益。因為高 的C02、N2含量和低的&含量’鼓風爐氣體的注入並非經 濟的。 在熔融-還原的工場裡，例如於DE 36 28 1〇2八丨中所 描述：為了將還原劑(主要為煤和煤磚)氣化，以及得到熔 Π原的鐵所需的熱’故將溫度為25。。且純度^ 95體 和：的氧、、:由噴嘴注入至熔融氣化爐中。熔融氣化爐⑽v) 的k鐵爐乳體係用於在固定床還原爐身㈣叫中或在流體 8 200827452 化床反應裔（WSR)中的間接還原。因為在FBRS或中 缺少氣體的使用，會得到高的煤或煤磚的比消耗（叩^丨仏 consumption)以及在輸出氣體中過量的高能量。 結合熔融氣化爐與還原反應器的操作提供了 7〇_9〇%之 鐵泥漿的波動金屬化。例如，在溶融氣化爐中的焦炭床和 熔鐵爐溫度的升高使得需要的氧量減少，目而也使還屬氣 體減v。因為攻樣的減少，纟固定床還原爐身或流體北床 反應中的金屬化也降低，因此，接著造成在熔融氣化爐 中焦炭床和熔鐵爐溫度的下降。然而，此造成較高的心 求且因而逖原氣體的量提高，以及再一次增加金屬化。 因㈣的控制系統，所卩，在熔融氣化爐中具有穩定的操 作疋不可犯的（尤其是因為煤的分解），因而導致較高的還 原劑比消耗。 在煤以氧的氣化期間，發生的絕熱火焰溫产 (RAFT)係高於 3〇〇〇〇r h田& ^ (δ兩上），因此，會促使Si02還® 成Si，且因而生鐵合呈 疋眾 王颂曰具有兩的矽含量。結果，常需要额 的再處理以達到所欲的 4汀攸的0·4-〇·5重量％之Si值。 經:純化之輪出褒辦太 ”體在1.5 barg具有下列典型的分析： C 〇 4 5 體積。/。、c 〇 3 〇 I# 籍 0/ 2體積％、h 19體積％、ϋ20 3體積％、 和Ν2 3體積〇/〇，1中兮 /、輪出氣體係由來自直接還原組件的 妓風爐氣體和由來自炫 > Ό A + s k㉚虱化爐的熔鐵爐氣體所組成。因200827452 IX. Description of the Invention: [Technical Field] The present invention relates to a method for producing a molten metal in which oxygen, a reducing agent and an iron system reduced in a reduction reactor are introduced into a smelting gasification furnace, The reducing agent is vaporized with oxygen, and the reduced iron is melted by the heat occurring in this case, the molten iron furnace gas from the melter-gasifier is used as at least a part of the reducing gas, and the reacted top gas is removed from The reduction reactor is removed; and the invention also relates to a plant for carrying out the method, having a reduction reactor, a melter-gasifier having an oxygen supply, and a supply system having a reducing agent, at least one of the 绫政田忠^1 ^ ^愫琛路攸攸攸攸 The melt gasifier supplies the molten iron gas to the reduction anti-column cry, the day $, 丨, ^ ^ k is suppressed and at least one line is used to remove the furnace from the reduction reactor Top gas. [Prior Art] t has been described, for example, in GB 883 998 A, in a blast furnace, various carbon-containing gases, such as natural gas, coke oven gas, etc., are injected through a tuyere or in the plane of the belly, in order to save coking coal and increase income. Because of the high CO 2 , N 2 content and low & content 'injection of blast furnace gas is not economical. In a melting-reduction plant, for example as described in DE 36 28 1〇2, 丨: in order to gasify the reducing agent (mainly coal and briquettes) and the heat required to obtain the molten iron The temperature will be 25. . And the purity of the liquid and the oxygen are: injected into the melter-gasifier by a nozzle. The k-iron furnace system of the melter-gasifier (10)v) is used for indirect reduction in the fixed bed reduction furnace body (4) or in the fluid 8 200827452 bed reaction family (WSR). Because of the lack of gas use in FBRS or in, high coal or briquettes consumption and high energy in the output gas are obtained. The operation of the melter-gasifier and the reduction reactor provides a fluctuating metallization of 7〇_9〇% of the iron slurry. For example, an increase in the temperature of the coke bed and the molten iron furnace in the melter-gasifier reduces the amount of oxygen required, and also reduces the gas to the v. Because of the reduction in the number of shots, the metallization in the reaction of the fixed bed reduction furnace or the fluid north bed is also reduced, thus causing a decrease in the temperature of the coke bed and the molten iron furnace in the melter-gasifier. However, this results in a higher desire and thus an increase in the amount of xenon gas and an increase in metallization. Because of the control system of (iv), it is unavoidable to have a stable operation in the melter-gasifier (especially because of the decomposition of coal), thus resulting in higher reductant ratio consumption. During the gasification of coal with oxygen, the adiabatic flame temperature production (RAFT) system is higher than 3〇〇〇〇rh field & ^ (δ 上上), therefore, it will promote SiO 2 to Si, and thus pig iron The co-presented Wang Hao has two sputum contents. As a result, it is often necessary to re-process the amount to achieve a Si value of 0. 4-〇·5 wt% of the desired 4 攸. The following typical analysis is performed at 1.5 barg: C 〇 4 5 volume. /, c 〇 3 〇 I# 0/ 2 vol%, h 19 vol%, ϋ 20 3 volume %, and Ν2 3 volume 〇 / 〇, 1 兮 /, wheel out gas system consists of hurricane gas from direct reduction components and molten iron furnace gas from 炫 gt + A + s k30 虱化化炉.because
為氣體過量，1以、范认、、， M /、 /、輸适供使用且使全部能量最佳化。 【發明内容】 9 200827452 因此，如開頭所描述，本發明的目標是具體指出一種 方法和-種工場，其中，除了增加的能量和原料之效能外， 生產率也會增加，同時獲得產物更好的冶金性質。 為了達到此目標，根據本發明，該方法的特徵在於將 至少部份經移除的爐頂氣引至溶融氣化爐内。因為此注 入，使在熔融氣化爐中作為還原劑之煤和煤磚的明顯節省 為可能的，其係被來自再循環氣體的還原物（co、h2)供應 所取代。再者’藉由直接降低火焰溫度來達到流體化床區 域，焦炭床的冷卻，其中該火焰溫度係㈣、煤磚或焦煤 人氧體組成分的吸熱反應和甲院的裂解所獲得。 有利地，在此情況中，壓縮再循環的氣體。 根據本方法-另外的有利變化，使再循環氣體於壓縮 弓丨至熔融氣化爐間被冷卻，較佳至3〇到$〇〇c，且減少 二氧化碳含量，較佳至2到3體積％。此優點為，在焦2 床中有較高的氣體量用於間接氣體還原，也就是說，更多 的遏原工作在熔融氣化爐中執行。 ^根據一另外的變化，若至少部分的再循環氣體只被壓 ^佑，至少另外部分的再循環氣體只被冷卻，且其二氧化碳 S夏減少，以及該壓縮氣體和該二氧化碳減少的氣體在引 至熔融氣化爐之前混合，則在熔融氣化爐中之性質的影響 可被更精確地測量。 為了此目的’也可使再循環和最多經冷卻的和二氧化 人減V的氣體在引至熔融氣化爐之前被加熱，較佳係使用 4分的再循環氣體流作為燃料氣體。藉由預熱再循環氣 200827452 體’可將可再循環的氣體量最大化，而不用使絕熱火焰溫 度（RAFT)降到低於不希望的低限，而帶來冶金上的缺點。 此造成使用原料之額外有利的還原，以及監控該程序的額 外可能性。 根據本發明，根據一方法的變化，可使至少一部份的 再循環氣體〃,L與較鬲的碳氫化合物重新組成，而使用另外 部分的再循環氣體流作為燃料氣體。For the excess of gas, 1 to, the standard, and M /, /, the transmission is suitable for use and optimizes the total energy. SUMMARY OF THE INVENTION 9 200827452 Accordingly, as described at the outset, the object of the present invention is to specify a method and a plant in which, in addition to the increased energy and the efficiency of the raw materials, the productivity is increased while obtaining a better product. Metallurgical properties. In order to achieve this object, according to the invention, the method is characterized in that at least a portion of the removed top gas is introduced into the melter-gasifier. Because of this injection, significant savings in coal and briquettes as reducing agents in the melter gasifier are possible, which is replaced by a supply of reducing (co, h2) from the recycle gas. Furthermore, by directly lowering the flame temperature, the fluidized bed area and the coke bed are cooled, wherein the flame temperature is obtained by (4), the endothermic reaction of the briquettes or coking coal oxygen components, and the cracking of the chamber. Advantageously, in this case, the recirculated gas is compressed. According to the method, in a further advantageous variant, the recycle gas is cooled between the compression bow and the melter gasifier, preferably to 3 Torr to 〇〇c, and the carbon dioxide content is reduced, preferably to 2 to 3% by volume. . This has the advantage that there is a higher gas amount in the coke 2 bed for indirect gas reduction, that is, more deuteration work is carried out in the melter gasifier. ^ According to an additional variation, if at least part of the recycle gas is only pressurized, at least another portion of the recycle gas is only cooled, and its carbon dioxide S is reduced in summer, and the compressed gas and the carbon dioxide reduced gas are cited. By mixing before the melter gasifier, the effect of the properties in the melter gasifier can be measured more accurately. For this purpose, it is also possible to recycle the gas which is recycled and at most cooled and deoxidized by V before being introduced into the melter-gasifier, preferably using a recycle gas stream of 4 minutes as the fuel gas. By preheating the recycle gas 200827452, the volume can maximize the amount of recyclable gas without lowering the adiabatic flame temperature (RAFT) below the undesired lower limit, with metallurgical disadvantages. This results in an additional advantageous reduction of the use of the raw materials and the additional possibility of monitoring the process. According to the present invention, according to a variation of a method, at least a portion of the recycle gas helium, L can be reconstituted with helium hydrocarbons, and another portion of the recycle gas stream can be used as the fuel gas.
在此情況裡，有利的是，重新組成的再循環氣體可和 僅被[及/或冷卻以及二氧化碳減少的氣體在引至炫融氣 化爐知混合。 根據-有利的方法變化，另外使在熔鐵爐氣體中共同 運輸的粒子被分離且再循環至熔融氣化爐中，而部分之僅 被壓縮和/或冷卻及二氧化碳減少的氣體流會被混合用於再 循環粒子的輸送。 根據本發明’根據一方法變化， J耗供控制在流體化 區域禋的理論絕熱火焰溫度，1 , 八係糟由再循環氣體之量和/ 或溫度和/或c〇2比例來控制，因 σ金私序的直接控制變 成可能的。 夂 由於廷些描述行為每個個 鈿人^ 〜扪了旎性，也因為這些的 、、且口’在流體化床區域有效的抑在 能的。 句欢的抆制理論絕熱火焰溫度是可 開頭所描述的工場特 支出來且通往熔融氣 根據本發明，為了達到此目標， 徵在於至少-目、線由爐了頁a的線路分 化爐内。 200827452 在此情況中，為了使著火或爆炸的風險最小化，氣體 的回線係與氧供給平行且儘可能遠離氧供給。 有利地，將壓縮器插入回線中。 體實例之特徵在於冷卻 縮器和氧供給之間，後 根據本發明，一工場的有利具 裝置和二氧化碳減少階段係插在壓 者也能夠減少或完全消除蒸氣含量 在此情況中，可使壓給哭山 ^ 史缓細斋的出口和二氧化碳減少階段In this case, it is advantageous that the reconstituted recycle gas can be mixed with the gas which is only [and/or cooled and reduced in carbon dioxide) in the flue gasifier. According to an advantageous method, the particles co-transported in the molten iron furnace gas are additionally separated and recycled to the melter-gasifier, while a part of the gas stream which is only compressed and/or cooled and reduced in carbon dioxide is mixed. Used for the transport of recycled particles. According to the invention 'according to a method, the J consumption is controlled by the theoretical adiabatic flame temperature in the fluidized zone, and the eight lines are controlled by the amount of recycled gas and/or the temperature and/or the ratio of c〇2, Direct control of the σ gold private sequence becomes possible.夂 Because the description of the behavior of each of the monks ^ ~ 扪 旎 , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , The adiabatic flame temperature of the sentence is the special expenditure of the workshop described at the beginning and is directed to the molten gas. According to the present invention, in order to achieve this goal, at least the line and the line are separated from the furnace by the furnace. . 200827452 In this case, in order to minimize the risk of fire or explosion, the return line of the gas is parallel to the oxygen supply and as far as possible from the oxygen supply. Advantageously, the compressor is inserted into the return line. The body example is characterized by a cooling cooler and an oxygen supply, and then according to the present invention, a field of equipment and a carbon dioxide reduction stage are inserted in the presser to reduce or completely eliminate the vapor content. In this case, the pressure can be made. To the crying mountain ^ Shishangzhai's export and carbon dioxide reduction stage
的出口通往一共同供給線，1通 ，、通到虱供給，再到熔融氣化 爐0 可將可再循環氣體的量最大化， 火焰溫度（RAFT)之冶金上的缺 藉由預熱再循環氣體， 而沒有因為過度降低絕熱 點’故在i缩器出口和二氧化碳減少階段出口之聚合處的 下游提供加熱I置。此提供了在原料使用上額外有利的減 少’以及監控程序的額外可能性。The outlet leads to a common supply line, one pass, to the helium supply, and then to the melter gasifier 0 to maximize the amount of recyclable gas, and the metallurgical defect of the flame temperature (RAFT) is preheated The recycle gas, without the excessive reduction of the hot spot, provides heating I downstream of the polymerization at the outlet of the i-retractor and the outlet of the carbon dioxide reduction stage. This provides an additional beneficial reduction in the use of raw materials and additional possibilities for monitoring procedures.
因為本發明有利之以燃料 特徵，一分支由壓縮器回線的 燃料氣體連接處，此可減少原 增加工場的效率。 氣體操作加熱裝置的進一步 上游散出且通到加熱裝置的 料的使用，且因此可進一步 有利地，可在壓縮器和氧供給之間插入重新組成器。 在此情況中，也可減少原料的消耗，其係因為根據一 有利的具體實例’-分支會由回線分支出I，且通到重新 組成器的燃料氣體連接處。 根據本發明另一工場的具體實例，其特徵在於使冷卻 裝置和二氧化碳減少階段以及重新組成器平行於回線的分 12 200827452 支’該平行的分支通往— 到炫融氣化爐。 共同供給線 其通到氧供給，再 較佳地，在至少一饺 々 提供一粒子 融氣化爐， ’载爐氣體的線路裡， 分離器，從其之粒子排 于排出處，粒子再循環通往炫 回線的刀支則流至粒子再循環處。 【實施方式】 ρ、左在之後的述敘中，將會藉由較佳的示範性具體實例和 奴附圖式來更詳細的說明本發明。 、 取隹使微粒或顆㈣彡狀的㈣石，若適#的話與未燒透的 ♦木物，進料至還原爐身J。產生於還原爐身丨的鐵泥漿 :!由排出裝置2引至熔融氣化爐3的上端。在熔融氣化爐 :底部，收集液態生鐵，以及在此上方的液態爐渣，其 在每個情況中較佳係經由特定的閥門不連續地被移除。: 儲存爐身4提供用於熔融氣化爐3的氣化劑，其較佳為煤 和/或煤磚，而在任何可能的情況中，該氣化劑係與被篩出 之小尺寸的鐵礦石混合，其中該小尺寸鐵礦石不可以除此 之外的方法用於還原程序中。一含氧氣體係經由在熔融氣 化爐3中較低部位的氣體線路5供應。 將產生的還原氣體經由線路6由熔融氣化爐3的 出’其在固體成分的熱氣體氣旋7中解放，且然後參τ<由 線路8進入還原爐身1，其中該固體成分特別是微粉媒和 細微顆粒之經除氣的煤。在經由線路8進入還原爐身i時， 硬原氣體以逆流方式流過鐵礦石和聚集物的管柱，且同時 13 200827452 將鐵礦石還原成鐵泥漿。 在熱氣體氣旋7中使經除氣的煤微粉分離，且其他微 粒含量係再循環至熔融氣域3,較佳係在進入後者之前 以微粉燃燒器氣化’其中該燃燒器係設置在溶融氣化爐3 的J中，且含氧氣體亦被輸送至此。 在避原爐身1上端經由爐頂氣線路9移除至少 =的還原氣體，以及在濕式洗氣…洗氣後，因為 〜的氧體’而運送作為輸出氣體和使全部的能量最佳化 用於濕式洗乳15 1 1巾洗氣後，讓用來調節工場壓力 ==體和輸出氣體混合，或者經由料12再播環作 —口^體而進人在熱氣體氣旋7上游的線路6。 斗寸別有利的是，你用$卜 便用至）部分經移除的爐頂氣，或者 出^之後’㈣至少部分藉由再循環進人程序本身的輸 ^ ’以恰好再循環且引域融氣化爐3。為了此目的， =環的爐頂氣被分支出去，由濕式洗氣器1〇的下游 ::線路13,且藉由壓縮器14壓縮，其中該壓縮器具有 的吸取壓力。有利地，甚至在混入輸出氣體之前， 器二要的還原氣體也可被分支以且再循環，自濕式洗氣 的下游通過另外的線路1 5。 根據第—個變化，於冷卻器16中中度冷卻至3〇·5〇。。 =於^場η中的叫含量降低i 2_3體積％之後，可將 盾|的爐頂'm溶融氣化爐3中以經由喷管a移除 二其中該喷管係引至氧喷嘴，而爐頂氣的 給儘可能的遠，且和氧供給平行。以此方式處理的二 14 200827452 體可被分支出去並混合於從熱氣體氣旋7再循環的粒+以 便傳达。除了藉由從再循環的爐頂氣提供像是c〇或只2的 還原物而節省煤和煤磚在熔融氣化爐中作為還原劑以外2， 因為直接的降低火焰溫度，亦可達到流體化床區域和焦炭 床的冷卻，其中直接降低火焰溫度係由於煤、煤磚或焦煤 與氣體成分之吸熱反應和甲院的裂解造成，下列為關鍵性 的反應： C + C02 -> 2 CO △H298 = +173 kJ/mol C + H20 c〇 + H2 AH298 = -fl32kJ/mol 4 ^ 2 H2 + C ^H298 = +74 kJ/mol 壓縮器14和（若適當的話）c〇2移除工場^與先前熱 交換器1“戈重新組成器/還原氣體溶爐21㈣設亦提供如、 :的優點：較高熔點表現，1因而增加生產率係可能的； 藉由減少使用還原劑，亦可達到減少每嘲生鐵@ %排出 比’以及，視煤、煤磚和焦煤之還原劑成本而$，降低操 作成本，1因而加快償還額外的投資成本係可能的。甚至 可設想在微粉燃燒器中用作氮的取代物。 在任何可能的情況中，爐頂氣亦可使用明顧的 ，引入。為了調節C02的含量，例如配合焦炭床或： 鐵爐的溫度變化，亦可混合兩個氣體流。 在移除co2之後，可視情況地加熱再循環的爐頂氣， 其中加熱可藉由還原氣體熔爐19 (對流的、再生的)、電加 15 200827452 熱、電漿燃燒器或熱交換器（使用經處理之氣體的顯熱，例 如，洗氣器上游的爐頂氣）…等。在此情況中，若使用還原 氣體加熱溶爐19，則經由線路20使用部分分支的爐頂氣 作為燃料氣體。 於引至熔融氣化爐3之前，藉由熱交換器加熱再循環 ^爐頂氣，較佳係使用濕式洗«L1 10上游之爐頂氣的熱 月匕因#需要較少的程序用纟量來冷卻爐頂氣，此提供了Because the present invention advantageously utilizes fuel characteristics, a branch is connected to the fuel gas line of the compressor return line, which reduces the efficiency of the original added worksite. The gas-operated heating device is further upstream and passes to the use of the heating device, and thus it may be further advantageous to insert a reconstitutor between the compressor and the oxygen supply. In this case, the consumption of the raw material can also be reduced because, according to an advantageous embodiment, the branch branches off from the return line I and leads to the fuel gas connection of the reconstitutor. A specific example of another plant according to the present invention is characterized in that the cooling means and the carbon dioxide reduction stage and the reconstitutor are parallel to the return line 12 200827452 'the parallel branch leads to the smelting gasifier. The common supply line leads to the oxygen supply, and preferably, at least one dumpling is provided with a particle melter, in the line of the carrier gas, the separator, the particles from which it is discharged, the particle recycling The knife that leads to the Hyun return line flows to the particle recirculation. [Embodiment] ρ, left in the following description, the present invention will be described in more detail by way of preferred exemplary embodiments and slave drawings. Take the sputum to make the particles or the (four) scorpion-like (four) stone, if appropriate, and the unfired ♦ wood, feed to the reduction furnace body J. The iron slurry generated in the reduction furnace body is introduced from the discharge device 2 to the upper end of the melter-gasifier 3. At the bottom of the melter-gasifier: liquid pig iron is collected, and the liquid slag above it, which in each case is preferably discontinuously removed via a specific valve. The storage body 4 provides a gasifying agent for the melter-gasifier 3, which is preferably coal and/or briquettes, and in any case where the gasifying agent is of a small size that is screened out Iron ore mixing, wherein the small size iron ore may not be used in the reduction process. An oxygen-containing system is supplied via a gas line 5 at a lower portion of the melter-gasifier 3. The produced reducing gas is liberated from the outlet of the melter-gasifier 3 via the line 6 in the hot gas cyclone 7 of the solid component, and then enters the reduction furnace body 1 from the line 8, wherein the solid component, in particular the fine powder Degassed coal of media and fine particles. Upon entering the reduction furnace body i via line 8, the hard raw gas flows through the column of iron ore and aggregates in a countercurrent manner, and at the same time 13 200827452 reduces the iron ore to iron slurry. The degassed coal fines are separated in a hot gas cyclone 7 and the other particulate content is recycled to the molten gas zone 3, preferably by gasification with a micropowder burner before entering the latter 'where the burner is set in a melt In J of the gasification furnace 3, oxygen-containing gas is also supplied thereto. At least the reducing gas is removed at the upper end of the original furnace body 1 via the top gas line 9, and after the wet scrubbing is performed, the oxygen is transported as an output gas and the entire energy is optimized after the scrubbing. After being used for wet washing, the water is used to adjust the pressure of the workshop == the body and the output gas are mixed, or the material is re-broadcasted through the material 12 to enter the hot gas cyclone 7 upstream. Line 6. It is advantageous for you to use the part of the top gas that has been removed, or to use the "recycle" of the process itself, at least in part, by recirculating the process itself. The domain melts the gasifier 3. For this purpose, the top gas of the = ring is branched off, downstream of the wet scrubber 1 :: line 13 and compressed by a compressor 14, wherein the compressor has a suction pressure. Advantageously, the reducing gas required for the second stream can be branched and recycled, even before mixing with the output gas, downstream of the additional scrubbing gas through additional lines 15. According to the first variation, it is moderately cooled to 3 〇·5 于 in the cooler 16 . . After the content in the field η is reduced by i 2_3 vol%, the top of the shield|m can be melted in the gasification furnace 3 to remove the second nozzle through the nozzle a, wherein the nozzle is led to the oxygen nozzle, and The top gas is as far as possible and parallel to the oxygen supply. The two 14 200827452 bodies treated in this manner can be branched and mixed with the particles + recycled from the hot gas cyclone 7 for communication. In addition to saving coal and briquettes as a reducing agent in the melter-gasifier by supplying a reducing material such as c〇 or only 2 from the recycled top gas, 2 can also be achieved by directly reducing the flame temperature. The cooling of the chemical bed area and the coke bed, in which the direct reduction of the flame temperature is caused by the endothermic reaction of coal, briquettes or coking coal with gas components and the cracking of the courtyard, the following are critical reactions: C + C02 -> 2 CO △H298 = +173 kJ/mol C + H20 c〇+ H2 AH298 = -fl32kJ/mol 4 ^ 2 H2 + C ^H298 = +74 kJ/mol Compressor 14 and (if appropriate) c〇2 remove workshop ^ With the previous heat exchanger 1 "Go reconstitutor / reducing gas furnace 21 (4) also provides the advantages of:: higher melting point performance, 1 thus increasing productivity is possible; by reducing the use of reducing agents, can also be achieved Reducing the cost per sneaker iron @% discharge ratio and the cost of reducing the reductant of coal, briquettes and coking coal, reducing operating costs, 1 thus accelerating the repayment of additional investment costs. It is even conceivable to use it in micronized burners. As a substitute for nitrogen. In any possible situation In the middle, the top gas can also be introduced and used. In order to adjust the content of CO 2 , for example, in combination with the temperature change of the coke bed or the iron furnace, two gas streams can be mixed. After removing the co2, it can be heated as appropriate. Recycled top gas, wherein heating can be by reducing gas furnace 19 (convective, regenerated), electric plus 15 200827452 heat, plasma burner or heat exchanger (using sensible heat of the treated gas, for example, In the case where the furnace 19 is heated by the reducing gas, a partially branched top gas is used as the fuel gas via the line 20. Before being introduced to the melter-gasifier 3 By heating the recirculating furnace top gas by the heat exchanger, it is preferable to use the hot-washing of the top gas of the upstream of the wet washing «L1 10 to reduce the top gas of the furnace by using less procedure. provided
、加秋序的此S效率之優點，其亦表示減少了程序用水果 的能量需求。料，減少了從爐頂氣排出進入程序用水的 熱，且其係經過冷卻塔流失或藉由蒸發造成水在系統中流 失’其必須持續地被補償。 或者，再循環的爐頂氣亦可與較高的碳氫化合物（例 如，天然氣）於重新組成器21中重新組成，而部分經過線 路22的爐頂氣係作為燃料氣體用於。 ^來自溶融氣化爐3之還原氣體的量，^氣體的再循 %其為增加的’係用於增加於還原反應階段1 (爐身或流 體化床)的生產和/或用於持續的金屬化。持續的金屬化係 错由使炫融氣化爐3和還原爐身i去耗而達到。在所有時 候都足夠之還原氣體的量允許在還原爐身！的持續金屬 化。因而在提供至溶融氣幻盧3的氧量上不需要任何大幅 度的變化以適應於熱經濟，因此造成心的焦炭床溫度、 較低的煤分解、且因而穩定㈣融氣化爐3之操作與低的 還原劑比消耗。熔融氣化爐操作的最佳化導致用於工場之 固定床還原爐身1 (FBRS)或用於流體化床反應H(WSR)的 16 200827452 還原劑較小需求量，此必要的量係全部藉由爐頂氣的再循 環來補償。 此外’因為較低的絕熱火焰溫度和較穩定的熔融氣化 爐操作，此造成快速調節的可能性、於生鐵中矽含量的降 低，以最小化在高溫下產生的矽還原，其根據如下的反應 式： ^The advantage of this S-efficiency in addition to the autumn order also means that the energy requirement of the fruit for the procedure is reduced. The heat that is removed from the top gas into the process water is reduced, and it is lost through the cooling tower or caused by evaporation in the system, which must be continuously compensated. Alternatively, the recirculated top gas may be reconstituted with a higher hydrocarbon (e.g., natural gas) in the reformer 21, and a portion of the top gas passing through line 22 may be used as a fuel gas. ^ The amount of reducing gas from the melter-gasifier 3, which is an increase in the amount of gas used to increase the production of the reduction reaction stage 1 (furnace or fluidized bed) and/or for continued Metalization. The continuous metallization is achieved by the consumption of the smelting gasifier 3 and the reduction furnace body i. The amount of reducing gas is sufficient at all times to allow for the reduction of the shaft! Continuous metallization. Therefore, no significant change in the amount of oxygen supplied to the molten gas is required to accommodate the thermal economy, thus causing the coke bed temperature of the heart, lower coal decomposition, and thus stabilization (4) the gasification furnace 3 The operation is consumed with a lower reducing agent. The optimization of the operation of the melter gasifier results in a smaller demand for the fixed bed reduction furnace body 1 (FBRS) for the plant or the 16 200827452 reducing agent for the fluidized bed reaction H (WSR), the necessary amount is all It is compensated by the recycling of the top gas. In addition, because of the lower adiabatic flame temperature and the more stable operation of the melter, this results in a rapid adjustment, a reduction in the content of niobium in the pig iron, to minimize the reduction of niobium produced at high temperatures, according to the following Reaction formula: ^
Si02 + 2C ^ Si + 2CO ΔΗ298 = + 690 kj/mol 因為爐頂氣的再循環只有1到100 ppm的H2s，所以 除了矽含量，亦可達到在生鐵中硫含量的減少，和單獨使 用煤、煤磚或焦煤時相比，實質地降低引入硫的發生。 最後，藉由氣體再循環，必須之喷嘴速率和流體化床 區域足夠之滲透、以及較低之熔化速率的設定皆係相當容 易的。 【圖式簡單說明】 此圖係顯示本發明之製造熔融材料的設備。 【主要元件符號說明】 1 :還原爐身 2 :排出裝置 3 ·您融氣化爐 4 :儲存爐身 17 200827452 5 :氣體線路 6 :線路 7 :熱氣體氣旋 8 :線路 9 :爐頂氣線路 I 0 :濕式洗氣器 II :濕式洗氣器 12 :線路 13 :線路 14 :壓縮器 15 :線路 16 :冷卻器 17 : 002移除工場 18 :喷管 1 9 :還原氣體熔爐 20 :線路 2 1 :重新組成器/還原氣體熔爐 22 :線路 18Si02 + 2C ^ Si + 2CO ΔΗ 298 = + 690 kj/mol Since the top gas is recycled with only 1 to 100 ppm of H2s, in addition to the cerium content, the reduction of sulphur content in pig iron can be achieved, and coal alone, Compared with coal briquettes or coking coal, the introduction of sulfur is substantially reduced. Finally, by gas recirculation, the necessary nozzle velocity and sufficient penetration of the fluidized bed zone, as well as lower melt rate settings, are relatively easy. BRIEF DESCRIPTION OF THE DRAWINGS This figure shows an apparatus for producing a molten material of the present invention. [Main component symbol description] 1 : Reduction furnace body 2: Discharge device 3 • Your gasification furnace 4: Storage furnace body 17 200827452 5: Gas line 6: Line 7: Hot gas cyclone 8: Line 9: Top gas line I 0 : wet scrubber II : wet scrubber 12 : line 13 : line 14 : compressor 15 : line 16 : cooler 17 : 002 removal workshop 18 : nozzle 1 9 : reducing gas furnace 20 : Line 2 1: Reconstitutor/Reducing Gas Furnace 22: Line 18