REACTOR AND PROCESS FOR GASIFYING AND/OR MELTING OF FEED MATERIALS

Abstract

A reactor enables gasification or melting of waste and additional feed materials. The reactor includes a co-current section with a plenum section and a feed section with a sluice. Feed materials are introduced into the reactor. The reactor further includes a buffer section and a pre-treatment section, which adjoins a bottom of the buffer section to create a cross-sectional enlargement. An intermediate section adjoins the pre-treatment section. An upper oxidation section adjoins a bottom of the intermediate section and includes tuyeres in at least one level. An upper reduction section adjoins a bottom of the upper oxidation section. The reactor further includes a gas outlet section. The reactor further includes a countercurrent section having a conical lower reduction section and a conical lower oxidation section adjoining the conical lower reduction section having at least one tuyere and at least one tapping.

Claims

1. Reactor (100) for gasifying and/or melting of feed materials, the reactor comprising a co-current section (110) comprising a plenum section (111) comprising a feed section with a sluice (112) through which the feed materials are introduced into the reactor (100) from above, a buffer section (113) located below the feed section (112), a pre-treatment section (114) that is located below the bottom of the buffer section (113) and which has a cross-sectional enlargement in the upper area and a narrowing cross-section in the bottom area so that a discharge cone (140) of the feed material can form, at least one gas supply means (119) which open in the pre-treatment section (114) in the region of the cross-sectional enlargement of the pre-treatment section (114) and through which hot gases can be fed to the discharge cone, and an intermediate section (115) that is located below the bottom of the pre-treatment section (114), an upper oxidation section (116) located below the intermediate section (115), the upper oxidation section (116) comprising tuyeres (117) arranged in at least two levels, wherein through the tuyeres (117) untreated or preheated oxygen and/or air is supplyable, and an upper reduction section (118) located below the upper oxidation section (116), a gas outlet section (120) comprising at least one gas outlet (121), wherein the cross-sectional area of the gas outlet section (120) is larger than the cross-sectional area of the upper reduction section (118) so that a cone-shaped bulk (141) can form, and a countercurrent section (130) comprising a conical lower reduction section (138) located below the gas outlet section (120) and a conical lower oxidation section (136) for accumulating on the bottom molten metal and molten slag, the conical lower oxidation section (136) being located below the conical lower reduction section (138) and comprising at least one tuyere (137) through which untreated or preheated oxygen and/or air is supplyable to the molten metal and molten slag, as to prevent solidification, and at least one tapping (131) for draining the molten metal and molten slag.

2. Reactor (100) for gasifying and/or melting feed materials of claim 1, wherein the upper reduction section (118) is fully arranged above the gas outlet section (120), the gas outlet section (120) is located below the upper reduction section (118) while providing a cross-sectional enlargement.

3. Reactor (100) for gasifying and/or melting feed materials of claim 1, wherein at least a portion of the upper reduction section (118) is arranged in the gas outlet section (120), the gas outlet section (120) having a cross-sectional enlargement with respect to the upper reduction section (118).

4. Reactor (100) for gasifying and/or melting of feed materials of any one of claims 1 through 3, wherein the volume ratio of the upper oxidation section volume to the plenum section volume is a ratio of 1:N volume units, wherein 4≤N≤20.

5. Reactor (100) for gasifying and/or melting feed materials of any one of claims 1 through 4, wherein the volume ratio of the upper oxidation section volume to the total volume of the upper reduction section volume and the plenum section volume is a ratio of 1:N volume units, wherein 7≤N≤20

6. Reactor (100) for gasifying and/or melting feed materials according to any one of claims 1 through 5, wherein the volume ratio of the countercurrent section volume to the total volume of the reactor is a ratio of 1:N volume units, wherein 1≤N≤8.

7. Reactor (100) for gasifying and/or melting feed materials of any one of claims 1 through 6, wherein the angle (ζ) of the conical lower reduction section and the angle (ζ) of the conical lower oxidation section are between 50° and 70°.

8. Reactor (100) for gasifying and/or melting feed materials of any one of claims through 7, wherein the pre-treatment section (114), the intermediate section (115), the upper oxidation section (116), the upper reduction section (118), the gas outlet section (120), the conical lower reduction section (138) and the conical lower oxidation zone (136) each comprise a refractory lining, wherein each refractory lining of each section comprises between two and six layers, each layer being made of a different material.

9. Reactor (100) for gasifying and/or melting feed materials according to claim 8, wherein the refractory lining of the upper oxidation section (116) comprises between three and six layers, each layer being made of a different material, the sum of the layer thicknesses having a thickness of at least 600 mm.

10. Reactor (100) for gasifying and/or melting feed materials of any one of claims 1 through 9, wherein the inner cross-sectional area of the intermediate section (115) is cylindrically constant or is tapered in the direction of the reactor floor, the inner cross-sectional area of the upper oxidation section (116) is cylindrically constant or is tapered in the direction of the reactor floor and the inner cross-sectional area of the upper reduction section (118) is cylindrical constant or widens towards the bottom of the reactor immediately following the upper oxidation section (116).

11. Reactor (100) for gasifying and/or melting feed materials according to any one of the previous claims, wherein at least one further tuyere (139) is arranged in a further level of the conical lower reduction section (138) or one further tuyere is arranged in a further level of the conical lower reduction section (138) and at least one additional tuyere is arranged in the upper reduction section (118).

12. Reactor (100) for the gasifying and/or melting of feed materials according to any one of the previous claims, wherein at least one further tuyere is arranged in a further level of the conical lower oxidation section (136).

13. Reactor (100) for gasifying and/or melting feed materials according to any one of the previous claims, wherein the internal cross-sectional area of the upper oxidation section (116) is formed such that the maximum distance from any point within a discharge bulk formed from feed materials to an outlet of at least one of the tuyeres (117) is less than a predetermined minimum distance, the minimum distance being less than 1.3 m at gas temperatures below 100° C. and at gas velocities below 100 m/s, less than 1.9 m at gas temperatures below 100° C. and at gas velocities between 100 m/s and 343 m/s, and less than 3.2 m at gas temperatures above 100° C. and/or at gas velocities exceeding 343 m/s, wherein the temperature and the gas velocities are provided at the outlet of the tuyeres (117).

14. Reactor (100) for the gasifying and/or melting of feed materials of any one of the previous claims, wherein an internal cross-sectional area of the upper oxidation section (116) is formed as a non-circular surface, in particular as a rounded rectangle, stadium, oval, ellipse, epicycloid, multi-circle, superellipse n>1, super-circle n=4 or as a polygon with five or more corners, such as a truncated square, a regular polygon or parallelogram.

15. Reactor (100) for gasifying and/or melting feed materials of any one of the previous claims, wherein only one gas outlet (121) is arranged in the gas outlet section (120).

16. Reactor (100) for gasifying and/or melting feed materials of any one of claims through 14 or 15, wherein the at least one gas outlet (121) according to one of the claims 1 to 14 or the only one gas outlet (121) according to claim 15 is arranged in the gas outlet section (120) at an angle (θ) of −60° to +90°.

17. Reactor (100) for gasifying and/or melting feed materials of any one of the previous claims, wherein the central vertical longitudinal axis of the co-current section (110) is arranged horizontally offset with respect to the central vertical longitudinal axis of the gas outlet section (120) and the gas countercurrent section (130).

18. Reactor (100) for gasifying and/or melting feed materials of claim 17 with reference to claim 15 or claim 16, wherein the only gas outlet (121) is located closer to the central vertical longitudinal axis of the gas outlet section (120) and the gas countercurrent section (130) than to the central vertical longitudinal axis of the co-current section (110).

19. Reactor (100) for gasifying and/or melting feed materials of any one of the previous claims, wherein a heat exchanger and/or a steam generator is coupled downstream to the gas outlet section (120) and gas suction means are coupled downstream to the heat exchanger or steam generator.

20. Reactor (100) for gasifying and/or melting feed materials of any one of the previous claims, wherein high-temperature gate valves are arranged in the shell of the upper oxidation section (116) and/or the conical lower oxidation section (136), the high-temperature gate valves being designed to allow the tuyeres (117) to be replaced during use of the reactor.

21. Method for gasifying and/or melting feed materials using a reactor (100) according to any one of claims 1 through 20, the method comprising the following steps: Providing feed materials into the co-current section (110), wherein the feed materials are fed via the feed section with a sluice (112), wherein the feed materials are preheated and pre-dried in the buffer section (113), wherein by the providing of the feed materials in the pre-treatment section (114), a discharge bulk having a discharge cone is formed, wherein the cross-section of the pre-treatment section (114) is enlarged with respect to the buffer section (113), Heating the discharge bulk in the pre-treatment section (114) to at least 800° C. by supplying air and/or oxygen and/or combustion gas through the at least one gas supply means (119), which open in the pre-treatment section (114) in the region of the cross-sectional enlargement of the pre-treatment section (114), in order to initiate pyrolysis at the surface of the feed materials or in the feed materials, the feed materials being fully pyrolyzed and fully dried in the subsequent intermediate section (115); Providing a lower lying hot upper oxidation section (116) by supplying untreated or preheated oxygen and/or air through the tuyeres (117) arranged in at least two levels, and Burning the pyrolysis products and feed materials, melting of metallic and mineral constituents, if any, and further coking the feed material residues in the hot upper oxidation section; Converting thermal energy into chemical energy in the upper reduction section (118), Providing a lower lying hot lower oxidation section by supplying untreated or preheated oxygen and/or air through the at least one tuyere (137) to the accumulated molten metal and molten slag present in the conical lower oxidation section to maintain the molten metal and molten slag in a molten state and draining the molten metal and molten slag through the at least one tapping (131) as necessary, Discharging the gases generated in the co-current section (110) through the at least one gas outlet (121) of the gas outlet section (120), and Discharging the gases generated in the countercurrent section (130) through the at least one gas outlet (121) of the gas outlet section (120), the gases formed in the conical lower oxidation section of the countercurrent section (130) flowing via the conical lower reduction section (138) to the gas outlet section (120).

22. Method of claim 21, wherein the gases generated in the co-current section and the gases generated in the countercurrent section are discharged by suction.

23. Method of claim 21, wherein an overpressure is generated in the co-current section, wherein the gases generated in the co-current section are discharged by overpressure.

24. Method of any one of claims 21 through 23, wherein nitrogen is injected to start the reactor.

25. Use of a reactor (100) for gasifying and/or melting of feed materials according to any one of the claims 1 to 20 for the recovery of energy.

Description

[0116] Further advantages, details and developments result from the following description of the invention, with reference to the attached drawings.

[0117] FIG. 1a shows a simplified cross-sectional view of an embodiment of an invented reactor.

[0118] FIG. 1b shows another simplified cross-sectional view of an embodiment of an invented reactor.

[0119] FIG. 2 shows a simplified cross-sectional view of a further embodiment of an invented reactor with the upper reduction section partially inserted into the gas outlet section.

[0120] FIG. 3 shows a simplified cross-sectional view of another embodiment of an invented reactor, where the central vertical longitudinal axis of the co-current section is horizontally offset from the central vertical longitudinal axis of the gas outlet section.

[0121] FIG. 4 shows the internal cross-sectional area of the upper oxidation section of a reactor, wherein the internal cross-sectional area is substantially formed as a circular area.

[0122] FIG. 5 shows the internal cross-sectional area of the upper oxidation section of a reactor, wherein the internal cross-sectional area is substantially designed as a stadium.

[0123] Like-numbered elements in these figures are either identical or fulfill the same function. Elements previously discussed are not necessarily discussed in later figures if the function is equivalent.

[0124] In the following FIG. 1a describes an embodiment of a substantially cylindrical reactor 100. In connection with the explanation of the details of the reactor, the method steps that take place during the treatment of wastes with organic components as feed materials in this reactor are also specified.

[0125] By using other feed materials, modifications of the reactor and/or method may be useful. In general, different feed materials can also be combined, for example by adding feed materials with a higher energy value (e.g. non-recyclable plastic, contaminated waste wood, car tires, or the like) during the gasifying/cracking/melting of non-organic feed materials.

[0126] The reactor 100 shown in FIG. 1a has three major sections, which are a co-current section 110, a gas outlet section 120 and a countercurrent section 130. The co-current section 110, the gas outlet section 120 and the countercurrent section 130 are surrounded by a, e.g. steel shell, which of obvious necessity has recesses for means for feeding feed materials and gases as well as discharging gases and materials. The co-current section 110, the gas outlet section 120 and the countercurrent section 130 are arranged substantially concentrically to each other (represented by the vertical dash-dot line passing substantially through the center of the reactor). In the co-current section a plenum section 111, an upper oxidation section 116 and an upper reduction section 118 are arranged. The plenum section 111 comprises a feed section with a sluice 112, whereby feed materials such as waste, water, car tires, additives or other feed materials are fed into the reactor from above via the feed section. The material flow of the solids is shown as a dashed arrow from top to bottom. A buffer section 113 is arranged below the feed section with a sluice 112. Below the buffer section 113 a pre-treatment section 114 for buffering and pre-drying the feed material volume is arranged below the buffer section, thereby creating a cross-sectional enlargement in the upper area and a narrowing cross-section in the bottom area so that a discharge cone (140) of the feed material can form from feed materials (indicated by the oblique dashed lines; between 114 and 119). Hereby, the bottom area corresponds to an inverted truncated cone with an angle α, wherein α is advantageously between 120° and 150°, preferably 135°. As further shown in FIG. 1a, two gas supply means 119 open in the pre-treatment section 114 in the region of the cross-sectional enlargement. Through the gas supply means 119 hot gases can be fed to the discharge cone. Pyrolysis can therefore take place on the surface of the discharge cone 140. The pre-treatment section 114 can also be made inert by burning off all oxygen stoichiometrically (as lambda may be approximately 1), e.g. controlled by a low-cost paramagnetic or chemical oxygen-analyzer. Hence, the expensive nitrogen-blanketing, as needed for other reactors may be avoided. Below the pre-treatment section 114 there is an intermediate section 115 which is equipped for final drying and complete pyrolysis. As shown in FIG. 1a the intermediate section 115 has a substantially cylindrical inner diameter. An essentially cylindrical oxidation section 116 adjoins the intermediate section 115, wherein in the upper oxidation section 116 the tuyeres 117 are arranged circumferentially in a plurality of levels (here three levels as shown). Untreated and/or preheated oxygen and/or air is added via the tuyeres 117, which increases the temperature to such an extent that all substances are converted into inorganic gas, liquid metal, coke, carbon and/or mineral slag. In the upper reduction section 118, which adjoins the upper oxidation section 116 and which is arranged substantially above a subsequent gas outlet section 120, the endothermic conversion of thermal energy into chemical energy takes place. At the same time, the gas flowing co-current with the solids (represented by a dotted arrow running from top to bottom), is generated starting from the plenum section via to the upper oxidation section and the upper reduction section 118 from top to bottom, and then introduced into the gas outlet section 120.

[0127] As shown, the gas outlet section 120 is connected to the upper reduction section 118, thereby creating a cross-sectional enlargement. As the cross-sectional area of the gas outlet section 120 is larger than the cross-sectional area of the upper reduction section 118, a cone-shaped bulk 141 can form. The gas produced is—approximately in cross-flow to the cone-shaped bulk 141—discharged in the gas outlet section 120 through at least one gas outlet 121 (shown by a dotted arrow running from left to right). It may be provided, for example, that four or more gas outlets 121 are distributed around the circumference (not shown), so that the gas produced in the co-current section and in the countercurrent section can be diverted radially in the cross-flow. The gas outlet 121 can be designed in such a way that the gas can flow downwards. The angle θ of the gas outlet is downwards between −60° and 0° (horizontal). Indicated in FIG. 1 is an angle with −30°. The gas outlet, however, can also be designed in such a way that the gas is discharged upwards (as depicted in FIG. 2), with an angle θ of the gas outlet being in particular 60°. Thus, depending on the application and constructability restrictions, any angle between −60° (sloped down), 0° (horizontal) and +90° (straight up vertically) can be designed.

[0128] Below the gas outlet section 120 the countercurrent section 130 is arranged, the countercurrent section 130 comprising the conical lower reduction section 138 and the conical lower oxidation section 136. As indicated in FIG. 1 the countercurrent section 130 is conical and tapered (narrows) towards the bottom of the reactor with an angle ζ, the angle ζ being between 50° and 70°, here approximately 60°. In the conical lower reduction section 138 the conversion of thermal energy into chemical energy also takes place.

[0129] Below the conical lower reduction section 138 there is, as shown, a conical lower oxidation section 136 in which at least one tuyere 137 and at least one tapping 131 are arranged. Through the at least one tuyere 137 untreated or preheated oxygen air and/or oxygen is introduced in order to oxidize the remaining carbonized material and to prevent the molten metal and molten slag from solidifying. The collection and discharge of molten metal and molten slag takes place in at least one tapping 131.

[0130] The gas generated in the conical lower oxidation section 136 and in the conical lower reduction section 138 also flows in countercurrent with the solid's flow through the bulk (represented by a dotted arrow running from bottom to top) to the gas outlet section 120, where it is discharged via the at least one gas outlet 121.

[0131] The reactor of FIG. 1a may have sectional internal volumes as disclosed for example 2 of table 1.

[0132] Of course, the reactor can also have other dimensions and thus other internal volumes, however, in this case the ratios are either essentially the same or within defined ranges. For this the volume ratio of the upper oxidation section volume to the plenum section volume can be a ratio of 1:N volume units, wherein N is a number greater than or equal to (≥) 4 and less than or equal to (≤) 20.

[0133] It may be advantageous that the gases produced in the co-current section 110 and in the countercurrent section 130 are discharged by suction. Furthermore, it can be advantageously provided that an overpressure is generated in the co-current section 110, whereby the gases produced in the co-current section 110 are discharged by overpressure.

[0134] Although the embodiment form specifically described above is particularly suitable for the treatment (gasifying, cracking and/or melting) of wastes, it will be obvious to the skilled person in the art that modifications of the reactor are necessary or expedient when other feed materials are used. In general, however, the reactor described above can also be used to treat hazardous wastes or feed materials with higher metal contents, whereby the gasification/cracking principle and the melting principle will predominate in some cases. Different feed materials can also be combined. For example, it is possible to add specific feed materials with a higher energy value (e.g. non-recyclable plastics, contaminated waste wood, tires, but also coal or the like) for melting non-organic feed materials.

[0135] The reactor 100 shown in FIG. 1b corresponds substantially to the reactor 100 shown in FIG. 1b, however in this embodiment the inner cross-sectional area of the intermediate section 115 widens (see angle β, wherein β is between 80° and 90°, here approximately 87°) in the direction of the reactor floor and the inner cross-sectional area of the upper oxidation section 116 tapers/narrows (see angle γ, wherein γ is between 80° and 90°, here approximately 85°) in the direction of the reactor floor. Further, as indicated by the angle δ, the cross-sectional area of upper reduction section 118 expands (see angle δ, wherein δ is between 50° and 70°, here approximately 60°) directly below the oxidation section 116.

[0136] The reactor 100 shown in FIG. 2 corresponds substantially to the reactor 100 shown in FIG. 1a, but in this embodiment the co-current section 110 with a portion of the upper reduction section 118 is inserted into the gas outlet section 120. As shown, the refractory lining (e.g. brick lining) of the upper reduction section 118 protrudes into the gas outlet section 120. Since the gas outlet section 120 has a larger cross-sectional area than the upper reduction section 118 and the at least one gas outlet 121 is located in the edge region of the gas outlet section 120, the gas produced in the co-current section 110 must bypass the refractory lining (e.g. brick lining) protruding into the gas outlet section 120 in order to reach the gas outlet 121, whereby less dust enters the following apparatus. The gas outlet 121 can be arranged in such a way that the gas is discharged upwards, with an angle θ of the gas outlet being between 0° and 90°, here depicted to be 60°.

[0137] The reactor of FIG. 2 may have sectional internal volumes as disclosed for example 1 of table 1.

[0138] Of course, the reactor can also have other dimensions and thus other internal volumes, however, in this case the ratios are either essentially the same or within defined ranges. For this the volume ratio of the upper oxidation section volume to the plenum section volume shall be a ratio of 1:N volume units, wherein N is a number greater than or equal to (≥) 4 and less than or equal to (≤) 20.

[0139] FIG. 3 shows another embodiment of the reactor 100. The reactor according to FIG. 3 corresponds substantially to the reactor 100 according to FIG. 1a, but in the gas outlet section 120 of the reactor only a single gas outlet 121 is arranged, the central vertical longitudinal axis of the co-current section 110 is arranged horizontally offset with respect to the central vertical longitudinal axis of the gas outlet section 120 and the gas countercurrent section 130 and the single gas outlet 121 is arranged closer to the central vertical longitudinal axis of the gas outlet section 120 and the gas countercurrent section 130 than to the central vertical longitudinal axis of the co-current section 110.

[0140] The central vertical longitudinal axes are shown as dash-dot lines in FIG. 3. As shown, the central vertical longitudinal axes are essentially arranged at the center of each section. As shown, the co-current section 110 is not arranged concentrically with respect to the gas outlet section 120. However, the gas outlet section 120 is arranged concentrically to the countercurrent section 130.

[0141] The advantage of this embodiment of the reactor 100 is that the surface area or the discharge area of the bulk is increased, which increases the discharge rate and reduces costs by reducing the number and/or size of downstream devices.

[0142] The reactor of FIG. 3 may have the sectional internal volumes as disclosed for example 3 of table 1.

[0143] Of course, the reactor can also have other dimensions and thus other internal volumes, however, in this case the ratios are either essentially the same or within defined ranges. For this the volume ratio of the upper oxidation section volume to the plenum section volume shall be a ratio of 1:N volume units, wherein N is a number greater than or equal to (≥) 4 and less than or equal to (≤) 20.

[0144] FIG. 4 shows a configuration of the internal cross-sectional area of the upper oxidation section 116 of a reactor 100, wherein the internal cross-sectional area is essentially formed as a circular area. The reactor 100 according to FIG. 1a, according to FIG. 1b, according to FIG. 2 or according to FIG. 3 can be a reactor with a circular internal cross-sectional area, as shown here. As shown, several tuyeres 117 are arranged (here only one level is visible) through which untreated or preheated oxygen and/or air are blown onto or injected into the bulk. The tuyeres 117 are distributed around the circumference of the circular area, so that preferably every point of the bulk can be supplied with the blown in or injected in untreated or preheated oxygen and/or air. Here, it is envisioned that the maximum distance from any point within the bulk formed from feed materials to an outlet of at least one of the tuyeres 117 is less than a predetermined minimum distance. The minimum distance is less than 1.3 m at gas temperatures below 100° C. and at gas velocities below 100 m/s, less than 1.9 m at gas temperatures below 100° C. and at gas velocities between 100 m/s and 343 m/s (sound velocity) and less than 3.2 m at gas temperatures above 100° C. and/or at gas velocities >343 m/s. Hereby, the temperature and the gas velocities (gas flow divided by PI/4×ID.sup.2) are given at the outlet of each of the tuyeres.

[0145] FIG. 5 shows a configuration of the internal cross-sectional area of the upper oxidation section 116 of a reactor, wherein the internal cross-sectional area is essentially designed as a stadium. The reactor 100 according to FIG. 1a, FIG. 1b, FIG. 2 or FIG. 3 can be a reactor with a stadium-shaped internal cross-sectional area. As shown, several tuyeres are arranged (here only one level is shown) through which untreated or preheated oxygen and/or air are blown in or injected in the bulk. The tuyeres 117 are distributed evenly around the circumference of the stadium area, so that preferably every point of the bulk can be supplied with the injected in untreated or preheated oxygen and/or air. Here, it is envisioned that the maximum distance from any point within the bulk to an outlet of at least one of the tuyeres 117 is less than a predetermined minimum distance. The minimum distance is less than 1.3 m at gas temperatures below 100° C. and at gas velocities below 100 m/s, less than 1.9 m at gas temperatures below 100° C. and at gas velocities between 100 m/s and 343 m/s and less than 3.2 m at gas temperatures above 100° C. and/or at gas velocities >343 m/s. Hereby, the temperature and the gas velocities (gas flow divided by PI/4×ID.sup.2) are given at the outlet of the tuyeres. This embodiment, for which the internal cross-sections of the co-current section may have, as the upper oxidation section 116, a stadium-shaped internal cross-sectional area, results in an increase in the diameter of the (horizontal) cross-section of the reactor and thus in an increase in capacity. Due to the non-circular cross-section, the bulk, in particular also the center of the bulk, is easily accessible for the untreated or preheated oxygen and/or air introduced via the tuyeres 117. A 2.1-fold increase in capacity is achieved through a stadium-shaped embodiment of the internal cross-sectional area of the whole reactor.

LIST OF REFERENCE NUMERALS

[0146] 100 Reactor [0147] 110 Co-current section [0148] 111 Plenum section [0149] 112 Sluice [0150] 113 Buffer section [0151] 114 Pre-treatment section [0152] 115 Intermediate section [0153] 116 Upper oxidation section [0154] 117 Tuyeres [0155] 118 Upper reduction section [0156] 119 Gas supply materials [0157] 120 Gas outlet section [0158] 121 Gas outlet [0159] 130 Countercurrent section [0160] 131 Tapping [0161] 136 Conical lower oxidation section [0162] 137 Tuyere [0163] 138 Conical lower reduction section [0164] 140 Discharge cone [0165] 141 Cone-shaped bulk