Abstract:
The invention relates to an apparatus and method for manufacturing molten irons. The method for manufacturing molten irons includes providing a mixture containing iron by drying and mixing iron ores and additives, passing the mixture containing iron through one or more successively-connected fluidized beds to convert the mixture into a reducing material that is reduced and calcined, forming a coal packed bed, which is a heat source in which the reducing material has been melted, charging the reducing material to the coal packed bed and supplying oxygen to the coal packed bed to manufacture molten irons, and supplying reducing gas exhausted from the coal packed bed to the fluidized bed. In the providing a mixture containing iron, exhaust gas exhausted from the fluidized bed is branched to dry at least one of the iron ores and the additives. The apparatus for manufacturing molten irons uses this method for manufacturing molten irons. Through the use of the invention, at least one of iron ores and additives is dried and conveyed to thereby enhance energy efficiency and minimize the amount of required equipment.

Description:
BACKGROUND OF THE INVENTION 
   (a) Field of the Invention 
   The invention relates to an apparatus and method for manufacturing molten irons, and more particularly, to an apparatus and method for manufacturing molten irons in which iron ores and additives are dried while being conveyed, and then by the sensible heat of exhaust gas of a fluidized-bed reactors, the iron ores and additives are charged to the fluidized-bed reactors to thereby manufacture molten irons. 
   (b) Description of the Related Art 
   The iron and steel industry is a core industry that supplies the basic materials needed in construction and in the manufacture of automobiles, ships, home appliances, and many of the other products we use. It is also an industry with one of the longest histories that has progressed together with humanity. In an iron foundry, which plays a pivotal roll in the iron and steel industry, after molten irons (i.e., pig iron in a molten state) are produced using iron ores and coals as raw materials, steel is produced from the molten irons then supplied to customers. 
   Approximately 60% of the world&#39;s iron production is realized using the blast furnace method developed in the 14 th  century. In the blast furnace method, coke produced using as raw materials iron ores and bituminous coal that have undergone a sintering process are placed in a blast furnace, and oxygen is supplied to the furnace to reduce the iron ores to iron to thereby manufacture molten irons. The blast furnace method, which is a main aspect of molten irons production, requires raw materials having a hardness of at least a predetermined level and grain size that can ensure ventilation in the furnace. Coke in which a specific raw coal that has undergone processing is needed as a carbon source used as fuel and a reducing agent. Also, sintered ore that has undergone a successive compacting process is needed as an iron source. Accordingly, in the modern blast furnace method, it is necessary to include raw material preparation and processing equipment such as coke manufacturing equipment and sintering equipment. Therefore, not only is it necessary to obtain accessory equipment in addition to the blast furnace, but equipment to prevent and minimize the generation of pollution in the accessory equipment is needed. The amount of investment, therefore, is considerable, ultimately increasing manufacturing costs. 
   In order to solve these problems of the blast furnace method, significant effort is being put forth in iron foundries all over the world to develop a smelting reduction process that produces molten irons by directly using fine coal as fuel and a reducing agent, and also directly using fine ores, which make up over 80% of the world&#39;s ore production, as an iron source. 
   The smelting reduction process typically uses a two-stage process of preliminary reduction and final reduction. The conventional molten iron manufacturing apparatus includes a fluidized-bed reactor that forms fluidized beds, and a melter-gasifier that forms coal packed bed and that is connected thereto. Iron ores and additives at room temperature are charged in the fluidized-bed reactor to undergo preliminary reduction. Since high-temperature reduced gas is supplied from the melter-gasifier to the fluidized-bed reactor, the iron ores and additives increase in temperature as a result of making contact with the high-temperature reduced gas. At the same time, 90% or more of the iron ores and additives at room temperature are reduced, and 30% or more of the same are calcined and charged to the melter-gasifier. 
   Coal is supplied to the melter-gasifier to form a coal packed bed, and the iron ores and additives at room temperature undergo smelting and slagging in the coal packed bed to be discharged as molten irons and slag. Oxygen is supplied through a plurality of tuyeres installed to an outer wall of the melter-gasifier such that the coal packed bed is burned and then the oxygen is converted into high temperature reduced gas, after which the high temperature reduced gas is supplied to the fluidized-bed reactor. Following reduction of the iron ores and additives at room temperature, they are exhausted outside. A temperature of the emitted exhaust gas is approximately 680° C., and a pressure thereof is 1.7˜2.5 bar. 
   In the case where iron ores are charged to the fluidized-bed reactor for reduction into reduced iron, in order to prevent the reduced iron from sticking to the fluidized-bed reactor and in order to prevent thermal loss in the melter-gasifier, additives such as limestone and dolomite are charged to the fluidized-bed reactor together with the iron ores. The additives are typically around 15˜20% of the total amount of the charged material. 
   Prior to charging the iron ores and additives to the fluidized-bed reactor, the iron ores and additives are dried in a drying apparatus to thereby ensure the free flow of these materials in the fluidized-bed reactor. To perform this operation, hot air is supplied to the drying apparatus to dry the iron ores and the additives. Since the iron ores makes up 80% or more of the combination with the additives, overall operating conditions are determined based on the requirements of the iron ore. However, because the additives have a grain size and density that are less than that of the iron ore, a significant amount of loss of the additives with a small grain size occurs if dried under the same conditions as the iron ore. Further, the drying apparatus frequently malfunctions since a substantial load is given to the same in order to realize favorable drying. Finally, 50% or more of the iron ores become fine ore of 1 mm or less to thereby clog the drying apparatus, thereby necessitating frequent production stoppages. 
   SUMMARY OF THE INVENTION 
   The invention has been made in an effort to solve the above problems. The invention provides an apparatus and method for manufacturing molten irons in which exhaust gas of a fluidized-bed reactor is used as conveying gas for conveying iron ores and additives, and, at the same time, its sensible heat is used to dry the iron ores and the additives such that costs associated with drying are reduced. 
   A method for manufacturing molten irons includes the steps of providing a mixture containing iron by drying and mixing iron ores and additives; passing the mixture containing iron through one or more successively-connected fluidized beds to convert the mixture into a reducing material that is reduced and calcined; forming a coal packed bed, which is a heat source in which the reducing material has been melted; charging the reducing material to the coal packed bed and supplying oxygen to the coal packed bed to manufacture molten irons; and supplying reducing gas exhausted from the coal packed bed to the fluidized bed. In the step of providing a mixture containing iron, exhaust gas exhausted from the fluidized bed is branched to dry at least one of the iron ores and the additives. 
   In the step of providing a mixture containing iron, at least one of the iron ores and the additives may be dried immediately prior to supply to the fluidized bed. 
   The step of providing a mixture containing iron may include discharging stored iron ores and additives; drying the iron ores and additives using separate heating air while vibrating the same; storing the dried iron ores and additives; and supplying the stored iron ores and additives to the fluidized bed. 
   Preferably, in the step of providing a mixture containing iron, an amount of branched exhaust gas is 20˜40% of an amount of exhaust gas exhausted from the fluidized bed. 
   Preferably, in the step of providing a mixture containing iron, at least one of the iron ores and the additives is conveyed and simultaneously dried. 
   Further, in the step of providing a mixture containing iron, a flow rate of exhaust gas is preferably 20˜30 m/s in the case where the iron ores are conveyed, and a flow rate of exhaust gas is preferably 10˜20 m/s in the case where additives are conveyed. 
   Preferably, in the step of providing a mixture containing iron, the iron ores are fine ores having a grain size of 8 mm or less. 
   The apparatus for manufacturing iron includes a conveying line for drying and conveying iron ores and additives; one or more fluidized-bed reactors that reduce and calcine the iron ores and additives supplied from the conveying line to perform conversion into reducing material; a melter-gasifier for charging the reducing material and receiving the supply of oxygen to manufacture iron; a reducing gas supply line for supplying reducing gas exhausted from the melter-gasifier to the fluidized-bed reactors; and a exhaust gas branch line for branching exhaust gas exhausted from the fluidized-bed reactors and supplying the same to the conveying line. 
   The apparatus may further include a hopper for each of the iron ores and the additives; and a bypass line connected to the hoppers and supplying the iron ores and additives to the conveying line. 
   The apparatus may further include a drying assembly for drying the iron ores and additives supplied to the hopper; a storage bin connected to the drying assembly and for storing the dried iron ores and additive; and a conveyor belt connected to the storage bin and providing the iron ores and additives to the fluidized-bed reactors. 
   Preferably, the conveying line is extended vertically, exhaust gas is supplied to a lower port of the conveying line, and the iron ores and additives are supplied to the conveying line at a position 1˜2 m higher than the supply position of the conveying line. 
   Preferably, a flow speed of the exhaust gas in the conveying line is 10˜30 m/s. 
   Preferably, an amount of branched exhaust gas is 20˜40% of an amount of exhaust gas exhausted from the fluidized-bed reactors. 
   Further, the iron ores are preferably fine ores having a grain size of 8 mm or less. 

   
     BRIEF DESCRIPTION OF THE DRAWINGS 
       FIG. 1  is a schematic view of an apparatus for manufacturing molten irons according to a first embodiment of the invention. 
       FIG. 2  is a schematic view of an apparatus for manufacturing molten irons according to a second embodiment of the invention. 
   

   DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS 
   Preferred embodiments of the invention will now be described in detail with reference to the accompanying drawings. It should be clearly understood that many variations and/or modifications of the basic inventive concepts may appear to those skilled in the present art. The embodiments are to be regarded as illustrative in nature, and not restrictive. 
     FIG. 1  is a schematic view of an apparatus for manufacturing molten irons according to an embodiment of the invention. The apparatus dries and conveys iron ores and additives, and supplies the same to a fluidized-bed reactor. 
   An apparatus  100  for manufacturing molten irons according to a first embodiment of the invention includes the main elements of a fluidized-bed reactor unit  20 , a melter-gasifier  10 , a raw material supplying unit  60 , and other accessory equipments. The fluidized-bed reactor unit  20  includes one or more fluidized-bed reactors having a fluidized bed therein, and acts to reduce and calcine iron ores and additives to reduced material. The reduced material is charged to the melter-gasifier  10 , which includes a coal packed bed therein, and oxygen is supplied to the melter-gasifier  10  to thereby produced molten irons. Reduced gas exhausted from the melter-gasifier  10  is used to reduce and calcine iron ores and additives through a fluidized-bed reactor, after which the reduced gas is exhausted to the outside. 
   Elements included in the apparatus for manufacturing molten irons will now be described in more detail. 
   The fluidized-bed reactor unit  20  includes a rock hopper  21  that is charged with an iron-containing compound in which dry iron ores and additives are mixed, and one or more fluidized-bed reactors having a fluidized bed therein. An intermediate charge means is provided in the rock hopper  21  shown in  FIG. 1 , and allows for iron ores and additives to be charged to the fluidized-bed reactor that is maintained at a pressure from a normal pressure to 1.5˜3.0 atmospheres. 
   The fluidized-bed reactors include a pre-heating reactor  23  for pre-heating the charged iron-containing compound, a preliminary reducing reactor  25  for performing preliminary reduction of the iron-containing compound pre-heated in the pre-heating reactor  23 , and a final reducing reactor  27  for performing final reduction of the iron-containing compound that is reduced in the preliminary reducing reactor  25 . In  FIG. 1 , although the fluidized-bed reactors are shown to include three stages, such a configuration is for illustrative purposes and the invention is not limited in this regard. Accordingly, a variety of different numbers of stages may be used for the fluidized-bed reactors. The iron ores and additives supplied to the fluidized-bed reactors forming a fluidized bed by contacting a high temperature reduced gas current therewith, and it is converted into a high temperature reduced material that is at a temperature of 80° C. or more, is 80% or more reduced, and is 30% or more calcined. 
   Although not shown in  FIG. 1 , to prevent scattering loss when reduced material discharged from the fluidized-bed reactors is directly charged to the melter-gasifier  10 , a hot compacting apparatus may be mounted between these elements. Further, a hot intermediate vessel  12  is provided for supplying the reduced material discharged from the fluidized-bed reactors to the melter-gasifier  10  to thereby make supply of the reduced material to the melter-gasifier  10  easy. 
   Lump coal or shaped coal realized by pressing fine coal is supplied to the melter-gasifier  10  to form a coal packed bed. The lump coal or shaped coal supplied to the melter-gasifier  10  is gasified by a pyrolysis reaction at an upper area of the coal packed bed and by a combustion reaction by oxygen at a lower area of the coal packed bed. Hot reduced gas generated in the melter-gasifier  10  by the gasified reaction is supplied in succession to the fluidized-bed reactors through a reduced gas supply line L 59 , which is connected to a rear end of the final reducing reactor  27 , to be used as a reducing agent and fluidized gas. 
   A dome-shaped empty space is formed to an area above a coal packed bed of the melter-gasifier  10 . The flow rate of gas is reduced by the empty space such that large amounts of fine powder included in the charged reduced material and fine powder generated as a result of an abrupt increase in temperature of coal charged in the melter-gasifier  10  are prevented from being discharged out of the melter-gasifier  10 . Further, such a configuration allows for absorbing of variations in pressure in the melter-gasifier  10  caused by irregular changes in the amount of gas generated as a result of directly using coal. The coal is gasified and removes volatile members therein while dropping to the bottom of the coal packed bed, and is ultimately burned as a result of oxygen supplied through tuyeres at the bottom of the melter-gasifier. The generated combustion gas raises through the coal packed bed, and is converted into high temperature reduced gas and exhausted to outside the melter-gasifier  10 . Part of the combustion gas is scrubbed and cooled while passing through water collecting devices  51  and  53  such that pressure applied to the melter-gasifier  10  is maintained within the range of 3.0˜3.5 atmospheres. 
   A cyclone  14  collects exhaust gas generated in the melter-gasifier  10  such that dust is again supplied to the melter-gasifier  10 , and gas is supplied as reduced gas to the fluidized-bed reactors through the reduced gas supply line L 59 . 
   Reduced iron drops to the bottom of the coal packed bed together with the coal to undergo final reduction and smelting by combustion gas and combustion heat generated by gasifying and combusting coal, after which the iron is exhausted to the outside. 
   The raw material supplying unit  60  that uses the exhaust gas exhausted from the fluidized-bed reactors includes an iron ore hopper  30 , an additive hopper  40 , and a conveying line L 57 , and acts to dry and convey iron ores and additives to the fluidized-bed reactor unit  20 . Iron ores and additives discharged respectively from the iron ore hopper  30  and the additive hopper  40  are supplied to the rock hopper  21  through the conveying line L 57  connected to an iron ores supply line L 30  and an additive supply line L 40 . Among the fluidized-bed reactors, part of the exhaust gas exhausted from the pre-heating reactor  23  is supplied to the conveying line L 57  through a branched exhaust gas branched line L 55 . The conveying line L 57  is extended vertically, and iron ores and additives are supplied to the conveying line L 57  at a location 1˜2 m higher than the supply position of exhaust gas. If iron ores and additives are supplied from a location 1˜2 m higher than the supply position of exhaust gas, scattering loss of the iron ores and additives occurring during drying and conveying is minimized, and the area of contact with the exhaust gas is maximized such that it is possible to dry and convey the iron ores and additives very efficiently. The supply position of the iron ores and additives from the conveying line L 57  shown in  FIG. 1  is used for illustrative purposes and does not restrict the invention. Accordingly, it is only necessary that the conditions described above be satisfied. 
   Iron ores and additives are dried and conveyed by the exhaust gas exiting the exhaust gas branched line L 55  that is connected to the lower port of the conveying line L 57  to be charged in the rock hopper  21 . The amount of exhaust gas branched and used in drying and conveying is preferably 20˜40% of the exhaust gas amount exhausted from the fluidized-bed reactors. If this amount of exhaust gas is used, an amount of dried and conveyed iron ores and additives is sufficient to manufacture molten irons. 
   If iron ores having a grain size of 8 mm or less is used, volume and density are relatively low such that a smooth supply to the rock hopper  21  is possible. Further, a suitable flow speed of the exhaust gas in the conveying line L 57  is 10˜30 m/s. If the flow speed of the exhaust gas is less than 10 m/s, the pressure at the bottom part of the conveying line L 57  increases to destabilize the flow of the exhaust gas. On the other hand, if the flow of the exhaust gas exceeds 30 m/s, scattering loss may occur. 
   Hence, by using the exhaust gas as a conveying gas of the iron ores and additives and drying the same by the sensible heat of the exhaust gas, the exhaust gas may be recycled to thereby save energy, and drying may be stably realized. Since drying and conveying occur simultaneously in the conveying line L 57 , the number of different types of equipment used for drying and conveying is significantly reduced. Especially, the amount of iron ores and additives supplied to the conveying line L 57  may be adjusted respectively by an iron ore valve V 30  and an additive valve V 40 , and the amount of the exhaust gas supplied to the conveying line L 57  may be adjusted by an exhaust gas valve V 55 . 
   In the apparatus for manufacturing molten irons according to the first embodiment of the invention, iron ores and additives are selectively supplied to the conveying line L 57  according to operating conditions to thereby realize drying and conveying. In the case where additives are supplied to the conveying line L 57  to realize drying and conveying, the valve V 40  is opened while the valve V 30  is closed such that only the additives are dried and conveyed: In this case, the flow speed of the exhaust gas supplied to the conveying line L 57  is preferably 10˜20 m/s. If the flow speed of the exhaust gas is less than 10 m/s, additives charged to a lower part of the conveying line L 57  are not fully transported in the conveying line L 57 , and some particles are accumulated in the lower part of the conveying line L 57 . Therefore, a pressure at the lower part of the conveying line L 57  is significantly increased such that flow in the conveying line L 57  is made unstable. On the other hand, a flow speed of the exhaust gas exceeding 20 m/s is not suitable since the grain size of the additives is too small. Here, the amount of iron ores that is processed is approximately 100˜130 tons/day, and the amount of additives processed is approximately 15˜30 tons/day. 
   Further, in the case where iron ores are supplied to the conveying line L 57  to be dried and conveyed, the valve V 30  is opened while the valve V 40  is closed such that only the iron ores are dried and conveyed. In this case, the flow speed of the exhaust gas supplied to the conveying line L 57  is preferably slightly greater. As a result of the greater particle size and density of the iron ores compared to the additives, the flow speed of the exhaust gas is preferably 20˜30 m/s. As described above, the iron ores and additives may be separately dried and conveyed as in the first embodiment of the invention, or may be mixed then dried and conveyed. 
     FIG. 2  is a schematic view of an apparatus for manufacturing molten irons according to a second embodiment of the invention. 
   An apparatus  200  for manufacturing molten irons according to the second embodiment of the invention shown in  FIG. 2  is identical to that of the first embodiment except for a raw material supply unit  65 . Accordingly, elements of the apparatus  200  for manufacturing molten irons identical to the elements of the first embodiment will not be described, and the explanation will be concentrated on the raw material supply unit  65 . 
   As shown in  FIG. 2 , the raw material supply unit  65  includes the iron ore hopper  30 , the additive hopper  40 , a drying assembly  61 , an iron ore storage bin  34 , an additive storage bin  44 , and conveyor belts  63  and  65 . 
   An iron ore supply line L 31  connected to the iron ore hopper  30  and an additive supply line L 41  connected to the additive hopper  40  are connected to the drying assembly  61  to supply iron ores and additives thereto. The drying assembly  61  supplies hot air to a lower area of its dispersing plate such that iron ores and additives are dried while being vibrated to a fluidized bed state. Iron ores and additives dried in the drying assembly  61  are stored respectively in the iron ore storage bin  34  and the additive storage bin  44 . The dried and stored iron ores and additives are transmitted by the first conveyor belt  63 . The first conveyor belt  63  is connected to the vertical second conveyor belt  65  such that the dried iron ores and additives are charged to the rock hopper  21 . 
   The second embodiment of the invention is used by connecting the conveying line L 57  to the above apparatus. Iron ores are supplied to the conveying line L 57  through an iron ore bypass line L 33  connected to the iron ore supply line L 31 , and additives are supplied to the conveying line L 57  through an additive bypass line L 43  connected to the additive supply line L 41 . Accordingly, iron ores and additives are formed into an iron-containing mixture and dried immediately prior to supply to the fluidized-bed reactors having fluidized beds. 
   Especially, the apparatus  200  for manufacturing molten irons of the second embodiment provides particular convenience by using the bypass lines L 33  and L 43  when the drying assembly  61  malfunctions or an excessive load is given to the drying assembly  61 . 
   That is, in the case where the drying assembly  61  malfunctions, valves V 31  and V 41  directed to the drying assembly  61  are closed, while valves L 33  and L 43  respectively mounted on the bypass lines L 33  and L 43  are opened such that iron ores and additives are directly supplied to the conveying line L 57 . Further, the valve V 55  is opened such that exhaust gas is supplied to the conveying line L 57  through the exhaust gas branched line L 55 , resulting in drying and conveying iron ores and additives to the rock hopper  21 . Accordingly, iron ores and additives are continuously dried and conveyed to enable charging to the fluidized-bed reactors, thereby allowing the manufacture of molten irons to be more flexibly performed. 
   In the case where a significant load is applied to the drying assembly  61 , the valves V 33  and V 43  are opened in a state where both the valves V 31  and V 41  directed to the drying assembly  61  are opened such that part of the iron ores and additives supplied to the drying assembly  61  are supplied to the conveying line L 57 . Therefore, the load applied to the drying assembly  61  is minimized. 
   The invention will be described in greater detail below through an experimental example. This experimental example merely illustrates the invention and is not meant to limit the invention. 
   EXPERIMENTAL EXAMPLE 
   Iron ores and additives of limestone were dried and conveyed through a conveying line. The properties of the iron ores and additives used in this case are as shown in Table 1 below. 
   
     
       
             
             
             
           
             
             
             
           
         
             
                 
               TABLE 1 
             
             
                 
                 
             
             
                 
               Iron Ores 
               Additives (Limestone) 
             
             
                 
                 
             
           
           
             
                 
             
           
        
         
             
               Composition 
               T. Fe 63.43 wt % 
               CaO 50.67 wt % 
             
             
                 
               FeO 0.24 wt % 
               MgO 2.44 wt % 
             
             
                 
               SiO 2  3.41 wt % 
               SiO 2  1.48 wt % 
             
             
                 
               Al 2 O 3  2.04 wt % 
             
             
               Water content 
               5~10 wt % 
               5 wt % or less 
             
             
               Grain size distribution 
               8 mm or less 
               4 mm or less 
             
             
                 
             
           
        
       
     
   
   Among the exhaust gas exhausted from the fluidized-bed reactors, 20˜40% was branched and supplied to the conveying line. The details of the exhaust gas supplied to the conveying line are as shown in Table 2 below. 
   
     
       
             
             
             
           
         
             
                 
               TABLE 2 
             
             
                 
                 
             
           
           
             
                 
               Composition 
               CO 20 vol %, H 2  21 vol %, CO 2   
             
             
                 
                 
               20 vol %, N 2  39 vol % 
             
             
                 
               Temperature and Pressure 
               680° C., 1.7~20.0 kgf/cm 2   
             
             
                 
               Flow rate 
               8000~9000 Nm 3 /hr 
             
             
                 
                 
             
           
        
       
     
   
   In the case where iron ores and the additives of limestone are each supplied to the conveying line, the size of the conveying line extended vertically, and the gas flow rate and pressure drops in the conveying line are as shown in Table 3 below. 
   
     
       
             
             
             
             
           
             
             
             
             
           
         
             
                 
               TABLE 3 
             
             
                 
                 
             
             
                 
                 
                 
               Inner Diameter 0.2 m, 
             
             
                 
               Size 
                 
               Height 40.0 m 
             
             
                 
                 
             
           
           
             
                 
             
           
        
         
             
                 
               Iron Ores 
               Gas flow rate 
               20~30 m/s 
             
             
                 
                 
               Pressure drop 
               0.30~0.50 kgf/cm 2   
             
             
                 
               Additives 
               Gas flow rate 
               10~20 m/s 
             
             
                 
                 
               Pressure drop 
               0.05~0.2 kgf/cm 2   
             
             
                 
                 
             
           
        
       
     
   
   Results of comparing water content prior to drying and following drying and conveying of the iron ores and additives in the conveying line are shown in Table 4 below. 
   
     
       
             
             
             
           
             
             
             
             
           
         
             
                 
               TABLE 4 
             
             
                 
                 
             
             
                 
               Iron Ores 
               Additives (Limestone) 
             
             
                 
                 
             
           
           
             
                 
             
           
        
         
             
                 
               Process rate 
               100~130 tons/day 
               15~30 tons/day 
             
             
                 
               Water content 
               5~10 wt % 
               5~6 wt % 
             
             
                 
               prior to drying 
             
             
                 
               Water content 
               3 wt % or less 
               1 wt % or less 
             
             
                 
               following drying 
             
             
                 
                 
             
           
        
       
     
   
   As shown in Table 4, when the iron ores and additives are dried through the conveying line, the amount of water content therein is significantly reduced, thereby indicating that conveying and drying are efficiently realized. 
   The invention has the advantage of being able to use fine ores and fine additives. That is, by using iron ores and additives of a minimal grain size, these materials may be conveyed and simultaneously dried using exhaust gas. 
   In the invention, since exhaust gas emitted from fluidized beds are branched and used, the amount of waste gas is reduced and energy may be reused. 
   In particular, by drying the iron ores and additives immediately prior to supplying the same to fluidized beds, pre-heating and reduction rates in the fluidized beds are further increased. 
   Also, since the invention may be applied to general drying assemblies, precautions may be taken against any problems that may occur with the drying assembly and load applied to the drying assembly may be dispersed such that the apparatus for manufacturing molten irons may be more flexibly operated. 
   A mixture containing iron is reduced using multiple stages of fluidized beds such that a reduction material that has been fully reduced and calcined may be obtained. 
   Although embodiments of the invention have been described in detail hereinabove in connection with certain exemplary embodiments, it should be understood that the invention is not limited to the disclosed exemplary embodiments, but, on the contrary is intended to cover various modifications and/or equivalent arrangements included within the spirit and scope of the invention, as defined in the appended claims.