MXPA98010160A - Device to produce iron sponj - Google Patents

Abstract

In a device for producing sponge iron from iron oxide agglomerates in a reduction body, a hot, carbon-containing, carbon monoxide reducing gas is used. The reduction gas is generated in a gas generator by partial oxidation of materials containing solid carbon and is in part supplied to the reduction body through several lateral reduction inlets (3) arranged at the same height around the circumference of the reducing body through several lateral reduction inlets (3) arranged at the same height around the circumference of the reduction body at the lower end of the reduction zone. The iron oxide agglomerates are introduced into the reduction body through the upper subarachnoe and discharged as sponge iron at its bottom end. The additional reduction gas inlets (15) formed as open down channels (11) extending from the outside towards the interior of the reduction body and / or formed as ducts extending obliquely downwards from the outside to the interior of the reducing body and / or formed as ducts extending obliquely downward from the outside to the interior of the reduction body and having open inner ends that are arranged below the plane of the lateral inlets of reducing gas. The reduction gas in this way can also supply the radial inner area of the reduction body, so that the introduction of powder by the reduction gas is not limited to the outer area of the bulk material of the reduction body.

Description

DEVICE TO PRODUCE SPONGY IRON The invention relates to a device according to the preamble of claim 1. With the reduction of the iron oxide agglomerates in a reducing body or stomach with a carbon monoxide-rich reducing gas and containing powder from a melting gasifier in a melting plant by reduction of iron ore, only a part of the hollow volume of -. Bulk material in the reduction body can be used to receive powder that is introduced with the reduction gas to the reduction body. Ac.-rrtás, of the powder that is introduced with the reduction gas with the plants in which the reduction body is connected to the melting gasifier instead of descending tubes, an additional amount of powder is introduced with the gas gasifier through from the descending tubes and the discharge devices to the lower area of the reduction body. The dust content of this gasifier gas is variable higher than that of the reduction gas that is introduced in a purposeful manner in the reduction body that has been previously dedusted in gas-type cyclones REF .: 28883 hot. In addition to this powder, the powder by virtue of the air separation of spongy iron discharged and in the case of calcined aggregates is further transported back to the reduction body by the upward flow of the gas gasifier. The total powder results in a more increased dusting of the lower area of the reduction body, in the pipeline, suspension of bulk material as well as an uncontrolled discharge of the spongy iron by the discharge devices. A particularly disadvantageous effect is that the powder which passes to the descending tuoos from the melting gasifier to the reduction body includes coal and tar-containing particles, which are only partially degassed as well as other components that result in pelleting. With a more intensive dusting of the iron oxide bulk material in the areas of intense movement and reduction gas inlet, respectively, the pressure difference between the melting gasifier and the lower area of the reduction body is increased and consequently , the highly dusted gasification gas influences upwards via the risers and the screw-type extractors, through which it has a direct access to the powder bulk material, lower in the center of the reduction body. Because of this increased pressure difference, the air separation affects the descending tubes more strongly, the dust content becomes higher and the bulk material in the lower area of the reduction body can be enriched with the circulation powder such that Due to the high operating forces within the bulk material enriched with powder, the completely low pressure differences are sufficient to provide suspension of the bulk material which results in well-known piping phenomena and the gas flow without disturbance comprising a very high dust content of the melting gasifier to the reduction body. A part of the powder is additionally transported in the lower area of the reduction body upwards in the reduction zone and leads to dusting of the bulk material and channeling therein as well. These intense dusting of the area of intense movement can occur if a powder with too small a size is introduced with the carbon by using a larger amount of carbon with the coal mixture that highly disintegrates at high temperatures when they appear to be highly increased temperatures such as gasifier which results in a greater disintegration of the coal with a more intensive disintegration of the ore in the reduction body and with a failure and partial failure of the powder recirculation, respectively. When these cases occur, the reduction powder requires more time until it is free of dust because a part of the powder is: a being again transported upwards through the channels formed. A part of the remaining hollow volume is filled by the fine particles that are introduced ccr- the raw material, and that originates partially in the reduction body by the reduction of the iron transporters and the calcination of the aggregates respectively. With this, the capacity of the reduction body is greatly limited since a large part of the hollow volume has to be maintained for the flow of the recirculating gas through the bulk material, therefore, the specific amount of the reduction gas desired at the minimum for the reduction of iron and the calcination of those close to you can be conducted through the reduction body that has moderate and highly limited pressure drops. With the overpass of a particular pressure drop that depends on the particle size, particle impression and hollow volume of the bulk material, well known "suspension" of the material occurs, in bulk as well as the channeling and cross flow of a part of the reduction gas through the channels without participating in the reduction process. Of the same, the result is a low degree of metalization, low carburation of the iron, and a low degree of calcination of the aggregates, under the performance of the plant as well as the quality of the crude iron. Therefore, for normal operation a specific minimum quantity of the reduction gas is required to be conducted through the reduction body without channeling and without suspension of the bulk material. This specific amount of reducing gas depends on the degree of oxidation of the reducing gas, the iron content of the iron oxides, the disintegration characteristics of the iron oxides used at low temperatures, the amount of disintegration characteristics of the iron oxides. aggregates as well as other factors and is approximately 1050 mn3 reduction gas per ton of iron oxide. Due to the high gas gasing temperatures and due to a low pressure drop inside the material of bulk material that serves as a gas blocking means for the gasification gas that is not dusted via the descending tubes with the falling of pressure is terminated by a large cross-section of the reduction body in the lower area, hot gas cyclones, lined with brick having a moderate efficiency dusting communities are used for the reduction gas such that this still additionally contains considerable amounts of dust also and therefore with the specific amount of the reduction gas there is a relatively low tolerance towards the top. By the introduction of reduction gas in the area of intense movement only in the circumference of the reduction body, the hollow volume portion of the bulk material is at a free available for the dust separations in the radial center of the reduction body. it is difficult to use whereby the specific amount of reduction gas can be conducted through a gas to a minor and the excenter ring of the bulk material within the portion of the gas inlets is dedusted more highly than necessary. Then, in this outer ring, the channeling and suspension begin. The larger the diameter of the reduction body the smaller the specific amount of the recirculation gas, it can be conducted through the reduction body without suspension and without channeling. From JP-A-62294127 it is previously known a device for producing foolish iron from iron oxides in the reduction body by using a reduction gas. This reduction gas is introduced into the reduction body through several gas inlets arranged at the same height around the circumference of a reduction body. Additionally, below the plane of these lateral gas inlets, another gas inlet for the reduction gas is provided at the radial center of the reduction body. This gas inlet is formed by the inner open system of a tube extending radially from the outside towards the center of the reduction body, with the tube being closed in its longitudinal direction and the reducing gas supplied via the external open end of the same. By this measure, a more uniform reduction of the iron oxides will be obtained by the cross section of the body. The problems involved with the introduction of a reducing gas containing dust are not explained here. Furthermore, US-A-4 118 017 discloses a device for producing flux iron from iron oxides in a reduction body by using hot reduction gas which is supplied at approximately the central height of the reduction body through several gas inlets placed around the circumference of the same. The reduction body is used at the lower end where this end comprises several truncated, inserted sections. In the outer circumference of each of these sections are located gas inlets for a cold reduction gas as a cooling gas for spongy iron. The problems involved with the use of a reducing gas containing dust are not considered here.

Therefore, it is an object of the present invention to improve a generic device since an increased reduction carburization of the spongy iron and are retained, the bulk material low in the powder content in the radially central area is used for the separation of the dust, a greater pressure drop occurs within the bulk material in the lower area of the reduction body such that hot gas cyclones having a higher pressure drop and therefore a greater degree of separation can be used to dust off the used gasification gas, as reduction gas, the amount of the gasification gas containing powder flowing through the descending tubes to the reduction body and is highly imitated, and by a uniform dusting of the whole bulk material no differences occur of additional pressure via the pipe connections and down tubes, respectively, between the melting gasifier and the lower part of the reduction rate. This object is solved according to the intention by the characteristics indicated in the characteristic portion of claim 1. Advantageous improvements of the device according to claim 1, result from the dependent claims. In the following, the invention is explained in more detail according to a modality shown in the Figures, in which: Figure 1 shows a vertical section through the reduction body; Figure 2 shows a horizontal section through the reduction body according to Figure 1 between the area of intense movement and the arsa of the ducts, respectively, for the additional introduction of reduction gas; Figure 3 shows a vertical section through a channel for feeding the reduction gas.

The cylindrical reduction body 1 is loaded from above, and is above the reduction zone, via the reduction tubes 4 where only two are illustrated in Figure 1 has a cross section that extends downwards and comprises in its upper area At a conicity of approximately 2 °, in its central portion B which is approximately 5 m high a conicity of approximately 0.5 ° and in its lower area C which approximately 2 m in height a conicity of 2-5 ° . Further, the reduction body comprises in its lower area several outputs of the funnel-shaped product 5 where only two are illustrated in Figure 1 and six are illustrated in Figure 2. The extensions are preferably funnel-shaped and the connections of tube 5a of the outputs of the product, respectively, running directly on the background formed in a slightly curved, horizontal order of the reduction body 1. The outputs of the product 5 are formed by deflectors of fireproof material, specifically the walls intermediate 9 and a conical block 10 in the radial center of the reduction body 1 having assemblies 6 cooled with nitrogen or cooled with agía. A support 12 cooled with water having a closure protection tube 13 and an insulation in the lower area between these tubes that are placed eccentrically as well as an open channel that is placed in the support 12 and formed as a half-pipe shell with the extended side walls, Figure 3 is shown. The supports 12 having channels 11 are placed above the outputs of the product 5 and are supported with their radially inner end in the assemblies 6 of the block IC of the fireproof material. As an alternative configuration, the inwardly sloping duct 8 is obliquely cut forwardly drawn in dashed lines in Figure 1. From the reduction gas of the outlet 'introduces the reducing gas into the channels 11 of and the ducts 8. , respectively, as indicated by the arrows 15. In the introduction portion of the reduction gas, the side walls of the channels 11 become deeper and the lining with brick is more strongly realized., in order to avoid qua the horizontal surfaces in which the deposited dust is allowed to remain. A greater gradient can be obtained when the gas connections 15 are placed laterally and obliquely to the support 12. Advantageously, at the bottom end of the connections of the tube 5a, a positive discharge device as shown in the Figures is placed Crazy for the spongy iron. A normal operation of this plant with the introduction of a reducing gas rich in carbon monoxide and containing dust, hot, only around the circumference in the reduction body 1 via the channels 2 of intense motion as well as the entrances 3 of reduction when using bulk mineral is only possible with smaller reduction bodies and when using pellets of good quality it is only possible with larger reduction bodies. In comparison, it is almost indispensable with large plant-s that operate with normal raw materials for part of the reduction gas that is going to be introduced into the radial center of the reduction body 1 to achieve a stable operation with a high performance interval and with more tolerance in the quantity of reduction gas, the content of the reduction gas powder in the operation of the raw material. It is left to consider a diameter of the reduction body of approximately 5 to 6 m as a limit between these two aspects. Having larger reduction bodies and by the use of a reduction gas rich in carbon monoxide contains powder, hot, in this way, in the lower area of the reduction body, several funnel-shaped outputs 5 are formed by diverters of fire-proof material, comprising intermediate walls 9 and conical block 10 in the central area and mounting 6 cooled with water or nitrogen are provided protruding through the bottom of reduction body 1 in the diverters. These assemblies serve as fixing devices for the support 12 cooled with water at the same time in which the channels 11 for the introduction of the reduction gas in the radially central area, predominantly, lower, of the reduction body 1 are suspended as well as in the case of serving as supports for the conduits 8. With these tube, funnel-shaped connections 5a preferably, brick-lined which are welded to the bottom of the reduction body 1 or which are secured with flange joints and extend to the outlet of the funnel-shaped product 5, an abrupt angle is provided which is required to slide the material and at the same time a greater height of the bulk material as a gas blocking material to reduce the pressure difference between melting gasifier and the reduction body 1 is provided. The introduction of a part of the reduction gas via the inlets 15 in the radially central area of the reduction body 1 must take place approximately 2 m below the plane of the lateral inlets 3 of gas reduction through at least each channel 11 made of heat-resistant steel and / or in the conduit 8 cooled with water, which is preferably placed directly above each outlet of the product 5 and above each intermediate wall of 9, respectively. The channels 11 for the introduction and distribution of the reduction gas are constructed as heat-resistant mite half-tube shells with extended side walls and are placed in the tube-like supports 12, cooled with water from above such that the sides Spreads of the half-tube shells form channels 11 and open in the downward direction. This configuration is advantageous since the channels 11 open, inclined slightly downwards, or horizontal, large, can not be clogged with material or powder, very large surfaces of the bulk material mitigate the introduction of the reduction gas and good conditions for separation of powder from the reduction gas introduced and to transport out the separated dust within the upper areas are provided in this area by bulk material that quickly adds down and is highly loose. For the reduction gas that contains dust, access to the areas of bulk material that is sprinkled to a small degree is allowed to score the complete cross-section of the reduction body 1. The bulkier part of the reduction body 1 that serves as a gas block medium and that it is not participating with the reduction process that occupies at least one third of the volume of the reduction body 1 is used for a high carburation and a residual reduction of the spongy hiarro when introducing a cooler reduction gas. Due to this reduction area and in this way the complete reduction body can be built smaller and easier, thus with the bodies of reduction of the average size and having a total weight of approximately 1 500 tons and as well as a larger section of the supports, this is a significant advantage. A higher carbon content and a higher metallization of the spongy iron reduces the energy need of the melting gasifier and participates in a more uniform operation and better quality of the spongy iron. Therefore, the reduction gas is left via the inlets 15 at a lower temperature than that of the remaining reduction gas to provide better conditions for the carburetion of the spongy iron in the lower area of the reduction body 1. A temperature of about 50 0 to 100 or less is to be considered as an optimum temperature for this partial flow of the reduction gas. An additional cooling down to about 650 ° 0 which is going to be an optimum for sponge iron carburation, however, would result in cooling in the center of the body and therefore a minor metallization in this area. By the introduction of a cooler reducing gas, despite the highly exothermic Bcadouard reaction, the bulk material is cooled within this area which is critical for pelleting and its formation is prevented in conjunction with bulk material from the relief weight of the column of the material above it by the supports 12 cooled with water and / or the conduits 8 cooled with water. As is well known, with the ncdulization of the calcined aggregates and the coal particles containing tar that are not completely degassed, degassing products that also contain water vapor that act both as a binder and main components of the pellets that have particles of Enclosed spongy iron and residual dust components, temperature of bulk material and its pressure are of significant importance. Above the pellets, once they are formed, the bulk material in the areas that are in the upper part of the reduction body 1 falls with a lower velocity. Intensive dusts and local overheating due to Boudouard reaction, exothermic, powerful, are also allowed to occur in the reduction zone in some areas of the same. The arrangement of the extractors by screw at the lower end of the pipe connections 5a is to be considered as an advantageous improvement. With this configuration, the reduction body 1 is not required to be cleaned during an exchange or a major repair of the screw type extractors, by which long nonproductive periods of production and high initiation costs are avoided. As a result of the proportion of channels 11 open downwards, the best conditions for the separation and transport of the separated powder are presented. The half-tube shells of the channels 11 having extended side walls can be manufactured integrally or with few welding seams in non-critical locations and serve as wear protection and thermal insulation for the water-cooled support 12. To minimize heat losses of the supports 12, they are provided with the additional protection tube 13 made of heat-resistant steel. The lower area that is loaded with a more intensive temperature between the two tubes is located eccentrically to each other and is filled with insulating fabric 14, and the protective tube 13 is preferably spaced in a particular manner spaced within the upper area transversely to the axis thereof, in order to avoid er deformation. virtue of different thermal loads. The scoortes 12 and / or the conduits 8 are supported within the wall of the reduction body 1 and in the assemblies 6 embedded within the intermediate walls 9 and the block 10 such that elongated and strong supports 12 and / or conduits are not required. 8 for the construction of larger reduction bodies. It is advantageous to use the mounts 6 embedded within the conical block 10 to support the tube supports 12 and the channels 11 as well as the mounts 6 embedded within the intermediate walls 9 to support the conduits 8. The water-cooled conduits 8 are placed in a sharp angle and cut obliquely at its front end to increase the blowing surface of the bulk material and to avoid clogging inside the ducts 8. With a taper selection of the reducing area of the reduction body 1, the amount of introduced powder, the swelling of the iron oxides, the disintegration characteristics and the granular composition of the iron oxides and the aggregates as well as the content of the carbon monoxide in the reduction gas are to be considered. In the area of the lateral inlets 3 for the reduction gas up to a height of approximately 2 m above it in which the greatest dusting and the greatest danger for the suspension of the bulk material occur, a high conicity of approximately 2 50 is chosen, in this way, and the bulk material is allowed to be open and receive the powder. An increased, additional reduction of the cross section to the top was advantageous for receiving the powder but will result in a greater increase in the specific pressure drop in the lower areas of the reduction body 1 by increasing the gas temperature and speed of gas, respectively. In this area, spontaneous iron carburation and heating of the entire area takes place by the highly exothermic Boadouard reaction, where the decrease in the amount of gas by spontaneous iron carburation is more than compensated by an increase in the amount of gas based on the intensive calcination of the aggregates. With a gas temperature increase of 80 ° C, the specific expression drop will increase up to 15% with a constant cross section. For this reason, a smaller taper angle of approximately 0.50 is chosen in this area that is approximately 3 to 5 m in height. A greater weight of the column of material existing above this speaks in favor of a small angle and a more specific pressure drop by more intensive dusting than in the upper areas. Because of this, a greater pressure drop and more intensive dusting in this area can be allowed. In the area above this, a conicity of about 2 0- will be considered as an optimum. The load of the reduction body 1 with the iron oxides which in this case are mixed with aggregates occurs via the distribution tubes. placed in the upper area within a circle that has its center in the longitudinal axis of the reduction body 1. The number of reduction tubes at least corresponds to twice the number of outputs of product 5. With higher reduction tables these Distribution tubes are mounted in two circles and in a larger number to minimize the segregation of the load and to avoid an intensified gas flow in the marginal area and in the center of the reduction body caused by an intensive M profile. The distribution tubes 4 are placed symmetrically towards the outlet of product 5. In this way, it is obtained for the bulk material below these distribution tubes 4 which are richer in fine granulation and fall with a lower speed than a thicker bulk material, to fall down with an increased speed through two respective distribution tubes 4 which are located directly above the two pick-up areas of the screw conveyors, specifically that of the respective channel 11 and the adjacent, intermediate walls 9 Of the same. The amount of reduction gas introduced via the inlets 15 into the central area of the reduction body 1 is advantageous with about 30% of the total amount of the reduction gas with medium size reduction bodies such that an external ring having an external ring is supplied. a larger surface with approximately 70% of the reduction gas via the intensely moving channel 2 and the inlets 3. with a 30% reduction in the amount of gas fed via the intense penetration channel 2, the loading of the bulk material also it is reduced by approximately 30% in this area that has the powder, so during normal operation, the channeling and suspension of bulk material will not wait any longer. A smaller portion of the reduction gas introduced via the downwardly opening channels 11 will flow into the outer ring as well, however, the main amount will flow in the radially central area of the bulk material of the reducing body 1 which is sprinkled to a lesser degree. With larger reduction bodies, the amount of reducing gas introduced into the radially central area of the reduction body will increase correspondingly. The introduction of the reduction gas into the central area of the reduction body via the water-cooled conduits 8 which are assembled with linings made of heat-resistant steel and which are directed obliquely downwards is another possibility to feed a part of the reduction gas in the radially central area of the reduction body 1, which, however, has the disadvantage that a relatively small flow surface will intensively spill the bulk material within the inlet area of the reduction gas which is disadvantageous in this area as well. For this reason, as a preferred alternative, the reduction gas in the central area of the reduction body 1 will be considered additional only via the channels 11 that open downwards. The addition of the reduction gas in the central area of the reduction body 1 via the conduits 8 is therefore preferably an alternative to be carried out with smaller reduction bodies. The supports 12 and the conduits 8, respectively, also convey a large portion of the weight of the column of the material that is above it such that they release and release the bulk material within the outputs of product 5 and the bridging does not occur inside. of these funnel-shaped areas that are narrow down. Channels 11 are mounted similar to star in parallel with each other. The feed pipes to these and / or the ducts 8 are cciocan with descending gradient, therefore, nc are clogged which is caused by dust deposits and the bulk material is pulled back during the pressure variation in the system. The extended side walls of the channels 11 that open downwards at perpendicular distances are provided with hardening pieces and distances 16, in this way, the contraction of the channel is prevented by compressing the walls that are in parallel to each other caused by the material in bulk.

It is noted that in relation to this date, the best method known by the applicant for carrying out the present invention is that which is clear from the present description of the invention.

Having described the invention as artecede, the contents of the following are claimed as property:

Claims (21)

1. Device for producing foolish iron from hyaline oxide agglomerates in a reduction body by using a hot, carbon-containing carbon monoxide-containing reduction gas, wherein the reduction gas is generated in a gas generator by oxidation Partially of the materials containing solid carbon and is supplied to the reduction body through several side inlets of reducing gas arranged at the same height around the ccference of the reduction body and at the lower end of the reduction zone, and the iron oxide compounds are introduced into the reduction cell through their upper area and discharged as sponge iron at their bottom end, characterized in that the additional reductant gas inlets formed at least as a open downward channel extending from the outside to the radially central area of the reduction body and / or at least one duct which extends from the outside obliquely downwards to the radially central area of the reduction body and having an open inner end, they are arranged below the plane of the lateral eneradas of the reduction gas.

2. The device according to claim 1, characterized in that the gas generator is a melting gasifier and the lower end of the reduction body is connected to the melting gasifier caoezal at least via a descending tuoo to supply spongy iron from the body of reduction to the fusion gasifier.

3. The device according to claim 1 or 2, characterized in that the seals of the funnel-shaped product are formed by deviators of fire-proof material in the lower area of the reduction body.

4. The device according to claim 3, characterized in that the cleaners are formed with radially extending intermediate walls and a conically extending block downwardly in the radially central area of the reduction body.

5. The device according to claim 3 or 4, characterized in that the assemblies for the inner ends of at least ur. channel and / or at least one conduit are embedded in the diverters.

6. The device according to any of the rei indications from 3 to 5, acterizado in which a respective channel is arranged pe above each product output.

7. The compliance device? -n any of claims 4 to 6, characterized in that a respective conduit is argulated above each intermediate wall.

8. The device according to any one of claims 1 to 7, characterized in that each channel is made of heat-resistant steel and is arranged below a water-cooled base which extends in the same direction and is suspended therein.

9. The device according to claim 8, characterized in that the channels are formed as half-tube shells that open downwards and have parallel walls extended downward and placed in the orts.

10. The device according to claim 8 or 9, characterized in that the scoortes are respectively covered with a protective tube and the space between them is filled with insulating fabric.

11. The device according to claim 9 or 10, characterized in that the height of the parallel walls decreases toward the center of the reduction body.

12. The device according to any of claims 1 to 11, characterized in that the channels are arranged as a star in parallel with each other.

13. The device according to any of claims 11 to 12, characterized in that the conduits are cooled with water and provided with a heat-resistant steel liner.

14. The device according to any of claims 11 to 13, characterized in that the feeding tubes have a downward gradient towards the channels and / or the conduits.

15. The device according to any of claims 3 to 14, wherein a screw extractor is provided at the lower end of each product outlet.

16. the device according to any of claims 1 to 15, characterized in that the reduction body increases from top to bottom with a graduated taper which is about 2.50 in the lower area from the lateral reduction inputs to approximately 2. m above this, it is from about 0.5 0 from about 2 m to about 5 m above this, and beyond from about 2.00.

17. The device according to any of claims 3 to 16, characterized in that in the upper area of the distribution body, distribution pipes are provided for charging with iron oxides and er. case with aggregates that the number is twice the number of product outputs and that they are arranged circumferentially in a circular and geometric manner towards them.

18. A method for producing foolish iron from ht-oxide agglomerates using a device according to claim 1, characterized in that the reduction gas is supplied via the channels and / or the ducts has a lower temperature than the retraction gas supplied at the lower end of the reduction zone.

19. A method according to claim 18, characterized in that the temperature of the reduction gas supplied via the channels and / or conduits is about 500 C less than the temperature of the reduction gas supplied at the lower end of the reduction zone.

20. A method for producing foolish iron from hyaluronic oxide agglomerates using a device according to claim 1, characterized in that the portion of the reduction gas delivered through the channels and / or ducts is approximately 30% of the total amount of reduction gas.

21. A method for producing foolish iron from a metal oxide agglomerate using a device according to claim 1, characterized in that the reduction gas supplied at the lower end of the reduction zeta is largely cleaned of the powder within the hot gas cyclones. SUMMARY OF THE INVENTION In a device for producing foolish iron from hyaline oxide agglomerates in a reduction body, a hot, carbon-containing carbon monoxide-containing reduction gas is used. The reduction gas is generated in a gas generator by partial oxidation of materials containing solid carbon and is in part supplied to the reduction body through several lateral reduction inlets (3) arranged at the same height around the ct circumference of the reduction body at the lower end of the reduction zone. Acids of iron oxide are introduced into the reduction chamber through their upper area and discharged as fluffy iron at their bottom end. The additional reduction gas inlets (15) formed as downwardly open channels (11) extending from the outside towards the interior of the reduction body and / or formed ce or ducts extending obliquely downwards from the outside to the inside of the reduction body and has open inner ends that are arranged below the plane of the lateral inlets of reducing gas. The reduction gas in this way can also be supplied to the radial inner area of the reduction body, so that the introduction of powder by the reduction gas is not limited to the outer area of the bulk material of the reduction body.