DE3441355A1 - METHOD AND DEVICE FOR REDUCING OXIDIC MATERIAL - Google Patents

Description

Andrejewski, Honke & Partner, patent attorneys in Essen * '"■ ·" ^J

The invention relates to a method and a device for reducing oxidic material.

The invention has set itself the task of one with regard to the process technology as well as with regard to the use of energy to realize optimal reduction process, which is a particularly easily controllable gas generation system and the procedure should also be flexible enough to that most of the reducing gas originally used to reduce the oxidic material is reused can be to generate fresh reducing gas.

The method for reduction according to the invention is identified of oxidic material essentially in that

a) a reducing gas consisting mainly of carbon monoxide and hydrogen from a carbon-containing one and / or produced hydrocarbon-containing starting material is, this starting material together with an oxidizing agent and optionally also one Slag builder into one. Gasification zone or a gasification chamber is introduced while simultaneously Heat energy is supplied from at least one plasma generator;

b) the reducing gas produced in this way to a temperature suitable for the subsequent reduction process brought and then in a reduction shaft furnace is initiated, which is to be reduced

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contains oxidic material, this gas being passed in countercurrent to the oxidic material ;.

c) essentially all of the water and dust-like particles from the after reduction of the oxidic material In view of its ability to reduce, partially consumed and oxidizing components such as Reducing gas containing carbon dioxide and water and dusty particles are removed, and the same is essentially fed back into the process.

d) at least a small partial flow of the partially consumed flow provided for return to the process Gas is withdrawn from the system to regulate the pressure of the entire gas flow; and

e) at least a small partial flow of the partially consumed gas provided for recirculation into the process is passed through a CO ₂ scrubber for the purpose of setting the H_ / CO ratio in the finished gas.

The pressure control is expediently carried out in the system a low gas emission. The gas flow released for pressure regulation is expediently flared or otherwise exploited, e.g. for drying the carbonaceous material used in the process.

The gas stream is preferably released after the gas leaving the reduction stage is at least partially replaced by water vapor and / or dust-like particles have been freed.

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The oxidizing agent used expediently consists of Oxygen and / or water and / or air and / or circulating gas, which is fed to the reaction zone in whole or in part by the plasma generator. Optionally, the oxidizing agent also be preheated.

Preferably, the carbon-containing and / or hydrocarbon-containing Starting material for generating the reduction gas in powder form and / or liquid form and / or lumpy form. used.

According to the invention, a combustion zone is expediently formed in the lower region of a shaft-shaped gas generator filled with solid carbonaceous material in lump form, with coke preferably being used as the filling. ^:

According to the invention, a partial flow of the partially consumed gas which contains CO is withdrawn from the reduction shaft furnace and into the gas generator filled with lumpy reducing material from above and at a suitable distance from the Combustion zone initiated to the heat in the manhole filling to exploit H «0 in EL · + CO and the carbon dioxide convert to carbon monoxide. A partial flow of this return flow of used reducing gas from the shaft furnace can also be used as Carrier gas for the introduction of a powdery carbonaceous material and / or a slag former together optionally used with sulfur acceptors immediately before the plasma generator. Part of this return flow

Andrejewski, Honke & Partner, patent attorneys in Essen "'

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of used REduction gas from the shaft furnace is also used as a carrier gas for the thermal energy supplied by the plasma generator used.

The CO _o content of the reflux gas to be fed back into the process is preferably adjusted by passing a desired amount of reflux gas through a CCL washer.

The reducing gas generated in the gas generator is expediently used freed of any sulfur impurities by adding suitable sulfur acceptors to the manhole filling be introduced and / or by passing the withdrawn gas through a sulfur filter. Alternatively sulfur acceptors can also be blown into the gasification zone will.

According to a further proposal of the invention, the temperature of the reducing gas withdrawn from the combustion zone of the gas generator is controlled ^{to a final temperature between 700 and 1000 ° C.}

a) by being mixed with such an amount of the partially used reducing gas from the reduction shaft furnace and / or

b) is subjected to cooling and / or

c) him such an amount of water and / or water vapor is added that

the desired temperature is reached.

I ■ AIQEE Andrejewski, Honke & Partner, patent attorneys in Essen * " ^vww

If only a small amount of this partially consumed reducing gas is used for temperature control, is this partially used reducing gas when passing through the immediately after the gas outlet from the upper Part of the reduction shaft furnace arranged gas scrubber cooled, so that the desired final temperature of the gas mixture can easily be achieved. However, if a strong reverse current is mixed with the freshly generated reducing gas, this return flow is expediently before the mixing heated with the reducing gas, for example using a plasma generator.

The CO ₂ content of the partial flow of recirculated furnace gas used to regulate the temperature of the reducing gas generated in the gas generator is set before this partial flow is mixed with the reducing gas.

_{Furthermore, H 3} S can be added to the finished reducing gas in order to prevent soot deposits.

The reducing gas is preferred by means of a two-stage Gasification generated in which the starting material is partially burned and at least partially in a gasification chamber is gasified, whereupon this gas mixture is converted into a bed of carbonaceous, lumpy material containing Is introduced and the physical heat content of the mixture from the gasification chamber in the Filling of carbonaceous, lumpy material is used to reduce the content of carbon dioxide and water in the

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To reduce gas, the gas generation process is controlled so that the withdrawn gas for a subsequent Process step has suitable temperature and composition.

A device according to the invention for the reduction of oxidic material with simultaneous generation of a suitable. Neten backflow or circulating gas for carrying out the method according to the invention is essentially characterized by a gas generator for reducing gas with a reaction chamber, at least one plasma generator with in the bottom of the The mouth of the reaction chamber, a shaft furnace optionally connected to the gas generator via a sulfur filter, which contains the oxidic material to be reduced, a gas outlet arranged in the upper part of this shaft furnace, a separator arranged next to this gas outlet for water and dust-like particles from the exiting gas stream and a subsequent gas outlet for pressure regulation and a main return line for the main part of this Gas to the gas generator, optionally via a COp washer.

In the main return line is expediently at least a compressor switched on.

The main return line is expediently connected to a CCL · washer. The CO ₂ scrubber preferably has a secondary line which is a direct extension of the main line for feeding circulating gas into the gas generator

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opens and also into a second main line, through which practically CO, -free circulating gas is mixed with the freshly generated reducing gas for the purpose of temperature control will.

Further features and special features result from the the following description of two exemplary embodiments with reference to the accompanying drawings; it shows

1 shows a schematic representation of an inventive Device with a single-stage gas generator; and

2 shows a schematic representation of a modified Embodiment of the device according to the invention with a two-stage gas generator.

The device according to Figure 1 has a reduction shaft furnace 1 for the reduction of oxidic, lumpy material. This shaft furnace 1 has a charging device for introducing oxidic lumpy material to be reduced. There is an inlet pipe at the bottom of the shaft furnace 3 for hot reducing gas, which consists essentially of carbon monoxide and hydrogen, this Gas is passed through the shaft furnace 1 in countercurrent. This outlet line 4 is with a separator 5 for Dust-like particles and water, a so-called gas scrubber, connected, from which the water and dust particles were removed and at the same time cooled gas flows to an outlet 6 provided for pressure regulation and then via a main return line 7 returned for reuse in the process

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will, as will be described later. The main return line 7 contains a compressor 8.

At least one plasma generator 10 opens into a shaft-shaped one Gas generator 11. A lance 12 for the supply of material required for gas generation also opens into this gas generator, while an outlet is provided at the bottom of the gas generator.

Downstream of the compressor 8, the return line 7 is connected to a CO _{3 scrubber.} This arrangement also has a secondary line 7a which opens into a direct extension of the return line 7 for circulating gas leading to the gas generator 11. It also opens into a second main return line 14 for circulating gas, this second line 14, however, _{supplying circulating gas, which is practically free of CO 3, to} the freshly generated reducing gas in order to regulate its temperature.

In principle, this arrangement offers the following functional conveniences:

The line 14 connected to the top of the inflator;

the main return line 7 can be connected to the gasification zone in the lower part via additional branch lines 15 and 15a Area of the gas generator 11 can be connected, i.e. circulating gas can before the plasma generator through the line 15 and after compression in the compressor 8a via the

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Line 15a fed in behind the plasma generator be to go through this;

Via a further branch line 17, the line 14 can be supplied with the reducing gas taken from the gas generator, which leaves the upper part of the gas generator via an outlet line 18, are connected, and via a further branch line 19 can connect the line 14 via a mixing chamber 20 with that of a sulfur filter 22 can be connected via a line 21 discharging reducing gas, and finally the line 14 with the reducing gas line 21 immediately before the Entry of the reducing gas into the reduction shaft furnace 1 can be connected.

In this way, the CO ^ content in the circulating gas can be flawlessly steer.

A feed line 9 for the oxidizing agent, for example in the form of oxygen and / or water and / or air and / or circulating gas, is directly connected to the plasma generator 10, optionally after preheating, this oxidizing agent fed to the reaction zone in the bottom of the gas generator 11 can be.

The device described above and shown in FIG works in principle as follows:

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The reduction gas for reducing the oxidic material in the Shaft furnace 1, which is introduced into the same via the inlet line, is in principle produced in the gas generator 11, by adding a carbonaceous and / or hydrocarbonaceous starting material together with oxidizing agents and is optionally fed to a gasification zone in the lower part of the gas generator 11 with slag formers, while at the same time thermal energy is supplied via at least one plasma generator 10. The reducing gas produced in this way is then in principle to one suitable for the subsequent reduction of the oxidic material in the shaft furnace 1 Bred temperature and blown into the shaft furnace 1 in countercurrent to the material to be reduced. After reduction of the oxidic material, the reducing gas contains oxidizing constituents such as carbon dioxide and water as well dusty particles, and is therefore partially consumed in terms of its reducing ability. The reducing gas is withdrawn through the gas outlet line 4 from the top of the reduction shaft furnace and then from water and dusty Particles in the gas scrubber 5 freed. A small part of the gas treated in this way in the gas scrubber 5, which was cooled at the same time, is then taken from the system via the gas outlet line 6 for the purpose of temperature control, while the main flow of this gas is fed back into the process through the return line 7, i.e. it can again can be used to generate reducing gas.

The gas generation in the shaft-shaped gas generator 11 can can be achieved in several ways. Powdery and / or

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.liquid, carbonaceous and / or hydrocarbonaceous Starting material can be blown into the gasification zone, for example through a feed line 12, in which case oxidizing agents such as oxygen or water vapor into the reaction zone through the plasma generator can be introduced. Recycle gas can enter the reaction zone upstream of the plasma torch via line 15 or the gas can be fed through the plasma generator via the Line 15a are supplied. The carbon-containing and / or hydrocarbon-containing starting material can also be in lumpy form Form can be fed via the gas generator's furnace, so that the gasification zone in the lower part of the with solid carbonaceous material is formed in lump form filled gas generator. Appropriately, as carbonaceous filling of the gas generator used coke.

In addition, water or part of the partially used reducing gas, which was withdrawn from the reduction shaft furnace 1 via the line 7 and the branch line 16, can also be introduced into the gas generator 11, which in this case is filled with lumpy reducing material. In this case, water or spent reducing gas is introduced above the gasification zone itself and at a suitable distance therefrom, whereby the heat of the shaft filling is used to convert H ₂ O to H, + CO and carbon dioxide to carbon monoxide.

The gas generation in the gas generator 11, 11 can also be achieved in this way be that powdery, carbonaceous material,

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is optionally blown in with sulfur acceptors and / or slag formers by means of steam or a carrier gas, which consists of partially consumed reducing gas of a partial flow that is taken from the reduction shaft furnace or from oxygen or a mixture of oxygen and water vapor.

The reducing gas generated in the gas generator 11 can be desulfurized by adding a suitable sulfur acceptor to the manhole filling, for example, or by blowing sulfur acceptors into the gasification zone or by transferring the gas generated in the gas generator the outlet line 18 is fed to a sulfur separation filter 22. Any remaining sulfur impurities are absorbed by the reduced metal oxide in the lower part of the reduction shaft furnace.

The reducing gas is generally maintained at a temperature range of 1000-1500 ⁰ C. However, such a hot reducing gas cannot be used directly for reduction in the reduction shaft furnace, so that its temperature must be reduced before it is introduced into the shaft furnace 1. This can be done in various ways within the scope of the invention.

For example, that flowing out of the gas generator 11 can Reducing gas via line 18 with a suitable substream be mixed by circulating gas. This is done via line 14, so that the temperature of the gas mixture between

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Line 14, so the temperature of the gas mixture is between 700 and 1000 ⁰ C. Alternatively, this mixing with a partial flow of the gas returned from the reduction shaft furnace 1 can be achieved in that the reducing gas is mixed after passing through the sulfur filter 22, ie on its way from the line 14 to the line 3. If a small partial flow of circulating gas is used from line 14, this should be sufficient to bring about the desired cooling of the reducing gas produced. However, if an extremely large amount of circulating gas is mixed with the reducing gas, such a strong current should preferably be heated to the precise temperature in the mixing chamber 20. This heating can take place, for example, by means of a plasma generator.

The temperature setting can also be achieved in that a partial flow of the gas generated through lines 21 and 19 is passed through a mixing chamber 20 acting as a cooler.

In addition, the required temperature setting can also at least partially by the supply of water and / or. Water vapor take place via a supply line 24. This measure also prevents the formation of soot deposits.

About the carburization potential of the reducing gas produced to control and to prevent methanation, suitable carbonaceous materials such as Methane, methanol and / or propane are fed in via line 25.

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Soot deposits can also be counteracted in that H ₀ S is blown in via line 26.

An important feature of the invention is that the COρ content can be continuously controlled in the used to control the temperature of the reducing gas circulated by the gas C0 _o -Wascheinrichtung.

The above-described generation of reducing gas in the shaft-like gas generator 11 can also be carried out in two stages Gasification can be carried out as shown in Figure 2.

The gas generation according to the invention offers important technical advantages. The gas generation can be carried out at such temperatures that the ash forms an easily manageable slag which is discharged without causing clogging problems in the process. The hydrogen content in the reducing gas can be controlled to a percentage suitable for the reduction process in that water and / or oxygen is blown in in a controlled manner in the gas generation stage and in the temperature control stage. An optimal reduction process and a conveniently controllable gas generation system are also achieved with regard to energy consumption. The control of the proportions of H ₀ O and CO ₀ in line 3 can consequently be carried out in such a way that the flow in lines 14 to 18 and 21 and 3 respectively. is also set in line 24.

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As already mentioned, the desulfurization can take place through a special sulfur filter can also be installed directly in the gas generator by removing the coke bed, for example is provided with suitable material or.indem suitable Material is blown into the gasification zone.

The modified embodiment of the invention shown in FIG. 2 Darge Instead of the single-stage gas generator 11 according to FIG. 1, the device has a two-stage gas generator 31. The device is otherwise constructed according to the same principles as the device shown in FIG.

The two-stage gas generator according to Figure 2 has a gasification chamber 29 and a shaft 30 filled with a bulk coke 31.

The gasification chamber 29 has a water-cooled outer jacket 32 and a refractory lining 33 and is preferably substantially cylindrical. Preferably a plurality of gasification chambers are also arranged around the shaft 30.

The shaft 30 has a lower slag outlet 34 and an upper gas outlet 35. Coke in lump form is the Well fed through a gas-tight feed 36 at the head. The mouth of the gasification chamber 29 is in the lower Part of the shaft, and the gas flows up through the bed of coke and out of the shaft through the gas outlet. at In the illustrated embodiment, the slag outlet 34 is used for the gasification chamber and the shaft together.

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In connection with the gasification chamber, at least one burner is provided which, in the exemplary embodiment shown, consists of a plasma generator 37. The plasma generator is connected to the gasification chamber through a valve 38 tied together. Oxidizing agent is fed into the plasma generator through a feed line 9 or can also be in front of the plasma generator be introduced through a feed line 39. The oxidizing agent can also consist of a carrier gas, which is passed through the plasma generator, or from a circulating gas which is supplied through the line 15a will. The hot turbulent gas which is generated in the plasma generator passes through the mouth 40 of the plasma generator into the gassing chamber. The carbonaceous fuel, preferably in powder form, is fed through a feed line 41 blown into an annular space 42 which is formed concentrically around the mouth of the plasma generator, and / or by a lance 43, which is also used for supplying further cut lengths such as slag formers can be.

Lances 44 and 45 are also provided in the shaft, through which further oxidizing agents such as, for example, H ₀ O, CO ₉ , can optionally be added in order to utilize the physical excess heat in the gas. This also allows the temperature and the composition of the gas to be controlled.

A first sensor 46 is located at the exit of the gasification chamber. arranged, while a second sensor 47 is seated in the gas outlet of the shaft. These sensors are used to measure the

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Temperature and / or for analysis of the gas. These two sensors enable the process to be controlled by controlling the external energy supplied and / or the material flows supplied to.control.

Fig.2 shows only one embodiment of a suitable one two-stage gas generator in a plant for carrying out the method according to the invention, with many other solutions are also conceivable. For example, the plasma generators be arranged tangentially on the circumference of the gasification chamber, so that a circumferential Flow is achieved. In addition, the gasification chamber can be arranged vertically to facilitate the separation of slag or the gasification chamber and the shaft can be provided with separate slag outlets.

In the two-stage gasification device according to FIG the starting material is partially burned and at least partially gasified in the gasification chamber, and on this The mixture obtained in this way is introduced into a shaft, which is filled with a bed of carbonaceous material contains lumpy form. The physical heat content of the gas mixture exiting the gasification chamber becomes This is used in the coke bed to reduce the carbon dioxide and water content in the gas. In this way the gas generation process can be controlled so that the outflowing gas is one with the subsequent process step without has further compatible temperature and composition.

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The hot carrier gas coming from the plasma generator receives expediently a rotary movement before it enters the gasification chamber is introduced, and the powdery carbonaceous fuel can be concentric around the hot gas stream which flows into the gasification chamber. By keeping the material in the gasification chamber receives a rotary movement, there is a protective layer of slag on the inner walls of the gasification chamber.

Naturally, the invention is in no way intended to be based on the exemplary embodiments described above, but can be based on various things Way to be modified. For example, gas can be generated by preheating the oxidizing agent from the outside Thermal energy are supplied.

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Claims (39)

Andrejewski, Honke & Partner Patent Attorneys Graduated Physicist Dr. Walter Andrejewski Graduate engineer Dr.-Ing. Manfred Honke Graduated Physicist Dr. Karl Gerhard Masch Attorney's files: 4300 Essen 1, Theaterplatz 3, Postf. 100254 62 482 / E-th November 9, 1984 Patent application SKF Steel Engineering AB P.O. Box 202 S-813 00 HOFORS, Sweden Process and device for the reduction of oxidic material. Claims. 1. A method for reducing oxidic material, characterized in that a) a reducing gas consisting mainly of carbon monoxide and hydrogen from a carbon-containing one and / or hydrocarbon-containing starting material is produced, this starting material together Andrejewski, Honke & Partner, patent attorneys in Essen with an oxidizing agent and optionally also a slag former in a gasification zone or a gasification chamber (29) is introduced, while at the same time thermal energy from at least one plasma generator (10; 37) is supplied; b) the reducing gas produced in this way to one for the subsequent reduction process brought to a suitable temperature and then in a reduction shaft furnace (1) is introduced, which contains the oxidic material to be reduced, this gas in countercurrent is passed to the oxidic material; c) essentially all of the water and dust-like particles from the after reduction of the oxidic material In view of its ability to reduce, partially consumed and oxidizing components such as Reducing gas containing carbon dioxide and water and dusty particles are removed, and the same is essentially fed back into the process; d) at least a small partial flow of the partially consumed flow provided for return to the process Gas is withdrawn from the system to regulate the pressure of the entire gas flow; and e) at least a small part of the flow to be returned to the process provided, partially used gas for the purpose of setting the Η ,, / CO ratio in the finished Gas is passed through a CO ^ scrubber. "'" 1441355 Andrejewski, Honke & Partner, patent attorneys in Essen 2. The method according to claim 1, characterized in that the gas stream withdrawn for pressure control is flared or is consumed for external purposes. 3. The method according to claim 1 or 2, characterized in that that the gas stream is withdrawn after the gas of water and dust-like particles leaving the reduction stage was released. 4. The method according to claim 1, characterized in that as an oxidizing agent for gas generation, oxygen and / or water and / or circulating gas is used and the gasification zone is supplied in whole or in part by the plasma generator (10; 37). 5. The method according to claim 4, characterized in that the oxidizing agent supplied by the plasma generator before the entry into the plasma generator (10; 37) is preheated. 6. The method according to any one of claims 1 to 5, characterized in that the carbonaceous and / or hydrocarbonaceous Starting material for generating the reducing gas in powder form and / or liquid form and / or lumpy form is used. 7. The method according to any one of claims 1 to 6, characterized characterized in that the gasification zone in the lower region of a solid, carbonaceous material in lumpy Form filled shaft-shaped gas generator (11; 31) formed will. Andrejewski, Honke & Partner, patent attorneys in Essen ''^; 8. The method according to claim 7, characterized / that the carbonaceous filling of the shaft (11; 31) is coke is used. 9. The method according to any one of claims 1 to 8, characterized in that water or a partial flow of the partially consumed reducing gas in the shaft furnace (1) filled with reducing material in lump form is introduced above and at a suitable distance from the gasification zone, in order to generate the heat in the shaft filling to convert H ₃ O into H ₂ + CO and the carbon dioxide into carbon monoxide. 10. The method according to any one of claims 1 to 9, characterized in that powdered carbonaceous material and / or slag formers, optionally together with sulfur acceptors, in the system immediately before the plasma generator (10; 37) is blown in with the aid of water or steam or a carrier gas, which from a partial flow of the partial used reducing gas, which has been withdrawn from the reduction shaft furnace (1), or consists of oxygen or air. 11. The method according to any one of claims 1 to 10, characterized characterized in that the carbonaceous starting material required for the generation of the reducing gas in the Gasification zone is introduced immediately in front of the plasma generator (10; 37). Andrejewski, Honke & Partner, patent attorneys in Essen ® '^{; !} - 5 ■ - 12. The method according to any one of claims 1 to 11, characterized characterized in that optionally additional oxidizing agent for generating the reducing gas and optionally likewise Slag formers and / or sulfur acceptors are introduced into the gasification zone in front of the plasma generator (10; 37) will. . 13. The method according to any one of claims 1 to 12, characterized characterized in that a mixture of carbonaceous, lumpy material and a suitable sulfur acceptor is used as a shaft filling above the gasification zone. ',: _. 14. The method according to any one of claims 1 to 13, characterized characterized in that the reducing gas generated in the gasification zone is desulfurized before it is introduced into the reduction shaft furnace (1). 15. A method according to any one of claims 1 to 14, characterized in that the reducing gas newly generated has a temperature between 1000 and 1500 ⁰ C. 16. The method according to any one of claims 1 to 15, characterized in that ^ the temperature of the reducing gas produced is ^{controlled to 700-1000 0} C, preferably 825 ° C, before it is introduced into the reduction shaft furnace (1). 17. The method according to claim 16, characterized in that the temperature of the hot reducing gas leaving the gas generator (11; 31), possibly after it has been desulfurized is controlled by Andrejewski, Honke & Partner, patent attorneys in Essen a) such an amount of the partially consumed reducing gas, which the reduction shaft furnace (1) was removed, mixed in and / or b) the hot reducing gas is cooled and / or c) such an amount of water and / or water vapor is added that the end temperature of the gas is between 700 and 1000 ^° C. 18. The method according to any one of the preceding claims, characterized in that a large partial flow of top gas once again brought into circulation from the reduction shaft furnace (1) is heated if necessary for the purpose of temperature control of the reducing gas before its addition to the reducing gas. 19. The method according to claim 18, characterized in that the heating is carried out by means of heat exchangers (20) in the furnace gas supply line. ■ 20. The method according to any one of the preceding claims, characterized in that the partial flow of is again in circulation brought furnace gas, which is used to regulate the temperature of the reducing gas generated in the gas generator (11; 31) is adjusted with respect to its CO "content before it is mixed with the reducing gas. Andrejewski, Honke & Partner, patent attorneys in Essen * "" ■ - ■■ - ' - 7 - 21. The method according to any one of claims 1 to 20, characterized in that the re-circulated Partial flow of used reducing gas from the reduction shaft furnace (1) by means of at least one compressor (8) the pressure required for the process is brought. 22. The method according to any one of claims 1 to 21, characterized in that a carbon support such as Methane, methanol and / or propane is added in order to increase the carburization potential of the reducing gas produced control and counteract methanation. 23. The method according to any one of claims 1 to 22, characterized in that as an antidote against soot deposits H_S is supplied. 24. The method according to any one of claims 1 to 23, characterized in that the reducing gas is generated by means of a two-stage gasification in which the starting material partially burned and at least partially gasified in a gasification chamber (29), whereupon the gas mixture obtained in this way into a shaft (31) containing a bed of carbonaceous, lumpy material is introduced and that the physical heat content of the mixture from the gasification chamber in the bed Lumpy material is used to reduce the content of carbon dioxide and water in the gas, whereby the gas generation process is controlled in such a way that the withdrawn gas is used for a subsequent process step has suitable temperature and composition. Andrejewski, Honice & Partner, patent attorneys in Essen ^ 25. Device for the reduction of oxidic material for Implementation of the method according to claim 1, characterized by a gas generator (11; 31) for reducing gas with a Reaction cannula, at least one plasma generator (10; 37) with a mouth located in the bottom of the reaction chamber, one to the gas generator optionally via a sulfur filter (22) connected shaft furnace (1), which contains the oxidic material to be reduced, one in the upper part of this Shaft furnace arranged gas outlet (4), a separator (5) arranged next to this gas outlet for the separation of Water and dust-like particles from the gas stream and a subsequent gas outlet (6) for pressure control and one Main return line (7, 14) for the main gas flow to the gas generator and / or for temperature control of the reducing gas generated in the gas generator. 26. Device according to claim 25, characterized in that the main return line (7, 14) with at least one Compressor (8) is provided. 27. Device according to claim 25 or 26, characterized in that the main return line (7, 14) to a COp washer connected. 28. Device according to claim 27, characterized in that the CO ₂ scrubber is provided with a secondary line (7a) which is a direct extension of the main return line (7) leading to the gas generator (11; 31) and also into a second main line ( 14) opens, through which the circulating gas, ■ - - 1441355 Andrejewski, Honke & Partner, patent attorneys in Essen ^> · - ■ - ■ »· whose CO ₂ content was adjusted with the freshly produced. Reducing gas for temperature control of the same is miscible. 29. Device according to any one of claims 25 to 28, characterized in that the second main return line (14) via the secondary line (17) and a first branch line (18) is connected to the upper region of the gas generator (11; 31). 30. Device according to any one of claims 25 to 29, characterized in that the main return line (7) via the secondary line (15a) and a second branch line (15) with the reaction zone in the lower part of the gas generator (11; 31) is connected. 31. Device according to any one of claims 25 to 30, characterized in that the plasma generator (10; 37) on a supply of oxidant for the direct passage of the optionally preheated oxidant through the plasma generator is connected to the reaction zone. 32. Device according to any one of claims 26 to 31, characterized in that the gas generator (11; 31) a Has slag outlet (13; 34). 33. Device according to any one of claims 26 to 32, characterized in that the gas generator (11; 31) a Filling made of carbonaceous, lumpy material, optionally with sulfur acceptors. Andrejewski, Honke & Partner, patent attorneys in Essen ^v ''"'" - 10 - 34. Device according to any one of claims 25 to 33, characterized in that the gas line between the gas generator (11; 31) and the sulfur filter (22) via a. Pipeline and a branch line to a partial flow Circulating gas can be connected. 35. Device according to any one of claims 25 to 34, characterized in that the reducing gas line (21, 3) between the sulfur separator (22) and the gas inlet of the reduction shaft furnace (1) with a temperature-regulating partial gas flow can be connected via a cooling device in the form of a mixing chamber (20). 36. Device according to claim 35, characterized in that for heating the partial flow of again circulated Gas in the mixing chamber (20) heat exchangers are arranged in the furnace gas return line. 37. Device according to any one of claims 25 to 36, characterized in that in the feed line (3) a Feed line (24) for water vapor opens. 38. Device according to any one of claims 25 to 37, characterized in that a supply line (25) for
a carbon carrier such as methane, propane and / or methanol opens into the feed line (3). 39. Device according to any one of claims 25 to 28, characterized in that a supply line (26) for HLS opens into the feed line (3).