NO844802L - PROCEDURE AND DEVICE FOR REDUCTION OF OXYDE MATERIAL - Google Patents

Description

The present invention relates to a method and a device for reducing oxide-containing material.

The purpose of the invention is to produce a process-technical and also from an energy point of view optimal reduction process with, among other things, an extremely easily adjustable gas generation system and with such flexibility in the process, that the main part of the reduction gas initially used for the reduction of the oxide-containing material can be reused for generation of new reducing gas.

This is achieved according to the invention by the initially described method mainly by,

a/ that a reduction gas containing mainly carbon oxide and hydrogen gas is produced from carbon and/or hydrogen carbon-containing starting material, whereby said starting material together with oxidizing agent and any slag formers is introduced into a gasification zone or gasification chamber with the simultaneous supply of heat energy from at least one plasma generator;

b/ that the reducing gas produced in this way is brought to a temperature suitable for the subsequent reduction and then introduced into a shaft furnace containing the oxide-containing material for the reduction and thereby made to flow countercurrently to said material deposited for reduction;

c/ that after the reduction of the oxide-containing material with oxidizing components, such as preferably carbon dioxide and water, as well as dusty particles, the reducing gas contaminated, and thus partially consumed with regard to its reducing power, is freed from water and dusty particles; and then essentially fed back into the process; d/ that at least a smaller partial flow of the aforementioned, partially consumed and calculated for reuse in the process gas in and before a pressure regulation of the total gas flow is taken out of the system and

e/ that at least a smaller partial flow of said, partially consumed and calculated for reuse in the process gas before adjusting the H^/CO ratio in the finished reduct ion gas is made to pass through a CC^ scrubber.

According to a suitable embodiment of the invention, the pressure in the system is regulated through a small gas discharge. Appropriately, the gas stream used for pressure regulation can be flared off or, for example, used for drying the carbonaceous material used in the process.

According to a preferred embodiment of the invention, the removed gas stream can be withdrawn after the gas emerging from the reduction step has been at least partially freed from water vapor and/or dust-like contaminants.

According to a suitable embodiment of the invention, oxygen gas and/or water and/or recycled gas are used as oxidizing agents in the gas generation, which are supplied to the reaction zone in whole or in part through the plasma generator. Optionally, the oxidizing agent can be heated in this way.

According to a suitable embodiment of the invention, the starting material containing carbon and/or hydrogen carbon used for the generation of the reducing gas is available in powder form and/or liquid form and/or as piece-shaped material.

According to the invention, the gasification zone is suitably formed in the lower part of a shaft filled with piece-shaped, solid carbon-containing material, whereby one can suitably use coke as a carbon-bearing filler in the shaft.

According to the invention, a partial flow of the partially consumed reducing gas withdrawn from the reduction shaft can also be introduced, whereby this partial flow of the partially used reducing gas, which also contains CO2, using a generation shaft filled with piece-shaped reducing material, can be introduced into the shaft above and at a suitable distance from the gasification zone, so that the heat in the shaft fill is used to convert E^O to H ? and CO respectively carbon dioxide in the partial stream of carbon monoxide. A partial flow of this return flow of spent reduction gas from the shaft furnace can also be used as carrier gas for the introduction of powdery, carbon-bearing material and/or slag formers as well as any sulfur acceptors immediately before the plasma generator.

According to a preferred embodiment of the invention, the carbon dioxide content in the return gas flow calculated for reuse in the process can be regulated by causing the return gas flow to the desired extent to pass through a CC^ gas scrubber.

According to a suitable embodiment of the invention, the reducing gas formed in the gas generation shaft can be freed from any sulfur compounds by providing suitable sulfur acceptors in the shaft fillers and/or by causing the gas withdrawn from the shaft to pass a sulfur filter. Alternatively, sulfur acceptors can be injected into the gasification zone.

According to a further embodiment of the invention, the temperature of the hot reducing gas withdrawn from the gasification zone in the gas generation shaft can be regulated

a/ through mixing with such a quantity of the partially consumed extracted from the reduction shaft, the reduction gas and/or

b/ by being subjected to a cooling and/or

c/ by mixing with such an amount of water and/or steam that the final temperature of the gas is between 700 and 1000°C. In cases where only a small part of the partially consumed reducing gas is used for temperature-regulating purposes - this partially consumed reducing gas is after all cooled when it passes through the gas scrubber immediately after the gas emission at the upper part of the reduction hunt - easily regulate the desired final temperature of the gas mixture . If, on the other hand, a large return flow is used for mixing in the generated reduction gas, this can be suitably heated before mixing with the newly generated reduction gas, for example with the help of the plasma generator.

According to a preferred embodiment of the invention, the partial flow of recycled shaft gas used for temperature regulation of the reducing gas formed in the gas generation shaft can be regulated with respect to its C02 content before mixing into the reducing gas.

According to a further embodiment of the invention, one can suitably add a carbon carrier, such as e.g. methane, methanol and/or propane to control the reducing gas "carburization potential" and to counteract methanization".

According to a further embodiment of the invention, H 2 S can be suitably added to the finished reducing gas to counteract soot formation.

According to a preferred embodiment of the invention, reducing gas can conveniently be formed by a two-stage gasification, whereby the starting material is partially combusted and at least partially gasified in a gasification chamber, after which the resulting gas mixture is introduced into a shaft which contains a bed of lumpy carbonaceous material and the physical heat content of the gas coming from the gasification chamber is used in the coke bed to reduce the carbon dioxide and water contained in the gas, whereby the gas generation process is controlled so that the outgoing gas has a temperature and a composition that is

passed to a subsequent process step.

The invention also includes a device for the reduction of oxide-containing material while simultaneously generating a gas suitable for recycling for carrying out the method and this device is mainly characterized by a generation device for reduction gas which contains a reaction chamber, at least one plasma generator opening into the reaction chamber, one to the generation device possibly via a sulfur filter connected to a shaft furnace which contains the oxide-containing material deposited for reduction, a gas discharge arranged in the upper part of the shaft furnace and a separator placed in connection with the gas discharge arranged to free the gas flow from water and dusty particles in addition to a subsequent gas discharge calculated for pressure regulation and a main feeder line for recycling the main gas flow to the gas generation device and/or temperature control of the reducing gas produced in the gas generation device, possibly via a CO2 gas scrubber.

According to one embodiment of the invention, there is at least one compressor in the main feed line.

According to a suitable embodiment of the invention, the main feed line is connected to a C02~ gas scrubber, whereby the C02 gas scrubber is appropriately equipped with a "bypass" line, which partly ends in a direct extension of the main feed line for the supply of return gas to the gas generation device and which partly passes into another main feed line intended to feed mainly carbon dioxide-free return gas to the intended mixing in the newly generated reducing gas during and before the temperature regulation.

Other characteristics of the invention can be seen from the specified special features in the attached claims.

In the following, the invention will be described in more detail with reference to two implementation examples shown in the attached drawings, where

figure 1 is a schematic view of a device formed according to the invention with a one-stage carburettor and

Figure 2 is a schematic view of an alternative device formed according to the invention with a two-stage gearbox.

In Figure 1, a reduction shaft suitable for the reduction of lumpy oxide-containing material is denoted by 1. The shaft 1 has a device 2 for feeding the lumpy oxide-containing material to be reduced. At the bottom of the shaft, there is an inlet line 3 for hot reduction gas, mainly consisting of carbon monoxide and hydrogen gas, and the aforementioned gas is led countercurrently through the reduction shaft 1 and then taken out through an upper gas outlet 4. The outlet line 4 is connected to a separator 5 for dusty particles and water , a so-called sinks, from which the gas cleaned of water and dusty particles and at the same time cooled passes past a gas discharge 6 designed for pressure regulation purposes and is returned via line 7 to a reuse in the process to be described in more detail below. In the line 7, there is at least one compressor 8. At least one plasma generator 10 opens into a gas generation shaft 11. 12 denotes a lance for the supply of material necessary for the gas generation and 13 denotes a device for draining slag from the gas generation shaft. After the compressor 8, the main feed line 7 is connected to a CC^ gas scrubber - this arrangement also includes a "bypass" line 7a, which partially ends in a direct extension of the main feed line 7 for the supply of return gas to the gas generation device 11 and which partially goes over into another main feeder line 14 designed to feed essentially carbon dioxide-free return gas to and before temperature control calculated mixing in the newly generated reduction gas.

In principle, the following functional possibilities are achieved through this: - via a first branch line 16, the main feeder line 7 can be connected to the upper part of the gas generation shaft; - via additional branch line 15 and 15a respectively, the main feeder line 7 can be connected to the reaction zone in the shaft 11's lower part, i.e. via line 15, return gas can be supplied in front of the plasma generator and via line 15a, after compression through the compressor 27, return gas can be made to pass through the plasma generator; - via a branch line 17, the feed line 14 can be connected to the reducing gas withdrawn from the gas generator, which leaves the upper part of the gas generator via a discharge line 18 and - via a further branch line 19, the feed line 14 via a mixing chamber 20 can be connected to it via a line 21 from a sulfur filter 22 the flowing reduction gas and finally the feed line 14 can be connected to the reduction gas line 21 immediately before the reduction gas enters the reduction shaft 1.

In this way, the CC^ content in the fed return gas can be regulated at all times.

A supply line 9 for oxidizing agent, for example in the form of oxygen gas and/or water and/or air and/or recirculated gas, is directly connected to the plasma generator 10, so that the oxidizing agent, possibly after preheating, can be brought to the reaction zone in the shaft 11's bottom.

The device shown in Figure 1 works in principle as follows: The reducing gas suitable for the reduction of the oxide-containing material in the shaft 1, which is introduced into the bottom of the shaft 1 via the gas inlet 3, is produced in principle in the gas generator 11 by a carbon and/or hydrocarbon-containing starting material together with oxidizing agent and any slag formers are introduced into a gasification zone and into the lower part of the gas generation shaft 11 with the simultaneous supply of heat energy from a plasma generator 10. The reduction gas produced in this way is then, in principle, brought to a for the subsequent reduction of the oxide-containing material in the shaft furnace 1 suitable temperature and is made to flow countercurrently to the material calculated for the reduction and the after the reduction of the oxide-containing material with oxidizing components, such as preferably carbon dioxide and water as well as dusty particles contaminated and thus partially consumed with regard to its reducing power auction gas is then taken out via the gas outlet 4 from the upper part of the reduction shaft and is then freed from water and dust-like particles in the gas scrubber 5. A small part of the gas treated in this way in the gas scrubber 5 and thereby also cooled can then in and before a pressure regulation of the system is drained from the system via the gas outlet line 6, while the main flow via the line 7 can again be supplied to the process, i.e. can again be used for the generation of reducing gas.

The gas generation in the shaft 11 can be carried out in many alternative ways. In this way, for example, powdery and/or liquid carbon- and/or hydrogen-carbon-containing starting material can be blown into the reaction zone through the supply line 12 and, furthermore, an oxidizing agent, for example oxygen gas or water vapor, can be introduced into the reaction zone through the plasma generator. Recirculated gas can be supplied to the gasification zone before the plasma burner via line 15 or said gas can also be supplied through the plasma generator via line 15a. The starting material containing carbon and/or hydrocarbon can also be supplied in piece form via the upper part of the gas generation shaft, so that the gasification zone is formed in the lower part of a shaft filled with piece-shaped solid carbonaceous material. Appropriately, you can too

use coke as carbon-bearing filler in the shaft.

During the gas generation, water or part of the partially consumed reduction gas drained from the reduction shaft 1 can also be introduced via the line 7 and the branch line 16 into the gas generation shaft 11, which is then filled with piece-shaped reduction material, i.e. introduced above and at a distance from the gasification zone itself and through this can the heat in the shaft filling is then used to convert F^O into H2+ CO, respectively carbon dioxide into carbon monoxide.

The gas generation in the shaft 11 can also be carried out by injecting powdered carbon-bearing material as well as any sulfur acceptors and/or slag formers with the help of water, water vapor or a carrier gas consisting of said partially consumed partial flow of the reduction gas withdrawn from the reduction shaft, or of oxygen gas or a mixture of oxygen gas and E^O (g).

The reduction gas generated in the shaft 11 can be freed from sulfur by the shaft filler containing a suitable sulfur acceptor or by injecting sulfur gas petors into the gasification zone or by supplying the gas produced in the shaft via the output line 18 to a sulfur separation filter 22. Any remaining sulfur compounds are taken up by the reduced metal oxide in the lower part of the reduction shaft.

The temperature level of the generated reducing gas is generally kept in a temperature range of between 1000 - 1500°C. However, such a hot reduction gas cannot be directly used for the relevant reduction in the reduction shaft and the temperature of the reduction gas must thus be lowered before it is introduced into the shaft furnace 1. This can be carried out in various ways within the scope of the invention.

For example, the reducing gas withdrawn from the gas generation shaft 11 via line 18 can be mixed with a suitable partial flow of recirculated gas from the shaft furnace, which is achieved via line 14 so that the temperature of the gas mixture is between approx. 700 and 1000°C. Alternatively, this mixing with the partial flow recirculated from the reduction shaft 1 can be achieved via a mixture in the reducing gas after the reducing gas has passed the sulfur filter 22, i.e. from line 14 to line 3. In those cases where a smaller partial flow of the return gas via the feed line 14 will presumably be sufficient to achieve the calculated cooling of the generated reducing gas. However, should a particularly large return gas flow be mixed into the generated reduction gas, such a large flow can be suitably heated to the right temperature in the mixing chamber denoted by 20. This heating can, for example, take place with the help of plasma generators.

The temperature regulation can also be carried out by a partial flow of the generated gas flowing through the lines 21 and 19 via a working mixing chamber 20 that cools.

The necessary temperature regulation can also be carried out, at least in part, by supplying water and/or steam via a supply line 24, through which soot formation is also prevented.

To control the "carburization potential" of the reducing gas formed and to prevent methanization, suitable carbon carriers - for example methane, methanol and/or propane - can be supplied via line 25.

In addition, any soot formation can be counteracted through the supply of E^S via line 26.

An important characteristic of the invention is that the CC^ content in the return gas used for temperature regulation of the reducing gas can be constantly regulated by the CC^ gas washing device.

The above-described generation of reducing gas in the shaft 11 can also be carried out using a two-stage

gassing.

Through the gas generation proposed in accordance with the invention, significant process engineering advantages are obtained. The gas generation can take place at such a temperature that the ash forms an easy-to-handle slag, which is drained off without causing clogging problems in the process. The hydrogen content in the reduction gas can be controlled to a content suitable for the reduction by a regulated injection of water and/or oxygen gas in the gas generation step as well as by temperature regulation. Even from an energy point of view, an optimal reduction process and an individually adjustable gas generation system are achieved. Regulation of the U^ O and the CG^ content in line 3 can thus be done by adjusting the current in lines 14 to 18 and 21 and 3 respectively as well as through line 24.

With regard to desulphurisation, as mentioned, instead of a separate sulfur filter, this function is built into the gas generation shaft itself by, for example, adding suitable materials to the cooking bed or injection into the gasification zone.

Figure 2 shows an alternative embodiment of the device according to the invention which, in contrast to the one-stage gas generator shown in Figure 1, contains a two-stage gas generator - otherwise the device is tied up in the same way as in the embodiment example according to Figure 1.

The two-stage gas generator shown in Figure 2 contains a gasification chamber denoted by 29 and a shaft denoted by 30 which exhibits a coke filling 31.

The gasification chamber 29 has an outer, water-cooled jacket 32 and a refractory lining 33 and is preferably designed substantially cylindrical. Preferably, several gasification chambers are arranged in connection with a shaft.

The shaft 30 has a lower slag outlet 34 and an upper gas outlet 35. Piece-shaped coke is supplied to the shaft through a supply device 36 opening at the top of the shaft, which is arranged to be gas-tight. The gasification chamber 29 opens into the lower part of the shaft from where the gas passes up through the coke bed and out through the gas outlet. In the embodiment shown, the slag outlet 34 is also common to both the gasification chamber and the shaft.

In connection with the gasification chamber, at least one burner is arranged, which in the embodiment shown consists of a plasma generator 37. The plasma generator is connected to the gasification chamber via a valve device 38. Oxidizing agent is introduced into the plasma generator through a supply line 9, alternatively oxidizing agent is supplied in front of the plasma generator through a supply line 39. The oxidizing agent can be a carrier gas which is passed through the plasma generator, alternatively a recirculated gas can be supplied through the line 15a. The hot, turbulent gas generated in the plasma generator is introduced into the gasification chamber through the plasma generator mouth 40. The carbonaceous fuel, which is preferably in powder form, is introduced through a supply line 41 into an annular gap 42 arranged concentrically around the plasma generator mouth and/or a lance 43 which can also is used for the supply of any additives such as e.g. slag formers.

In the shaft, lances 44, 45 are also arranged for the supply of any additional oxidizing agent, such as e.g. t^O, CO2, for utilization of physical excess heat in the gas. This also makes it possible to regulate the temperature and composition of the gas.

In the end of the gasification chamber lying at the coke filling, a first key device 46 is placed and in the gas outlet 35 from the shaft, another key device 47 is arranged, for temperature measurement and/or gas analysis. With the help of these two key devices, the process can be controlled by regulating the supplied external energy and/or by

iation of the added material flows.

Figure 2 thus exclusively shows an embodiment of a suitable two-stage carburettor in the device for carrying out the method according to the invention. Many other solutions are conceivable. For example, the plasma generators can be arranged tangentially on the periphery of the gasification chamber and then arranged so that a circulating flow is achieved in the gasification chamber. Furthermore, to simplify the slag separation, the gasification chamber can be arranged vertically. Likewise, the gasification chamber and the shaft can utilize separate slag outlets. When using the two-stage gasification shown in Figure 2, it is thus achieved that the starting material is partially combusted and at least partially gasified in the gasification chamber and that the resulting mixture is introduced into a shaft containing a bed of piece-shaped, carbonaceous material, whereby the physical heat content of the gas mixture coming from the gasification chamber is used to reduce the content of carbon dioxide and water in the gas in the coke bed. Through this, the gas generation process can be controlled so that the outgoing gas exhibits a temperature and composition that is well adapted to a subsequent process step.

Appropriately, the hot carrier gas coming from the plasma generator can be given a rotating movement before it is introduced into the gasification chamber and the powdered carbonaceous fuel can thereby be introduced concentrically around the hot gas flowing into the gasification chamber. When the material in the gasification chamber is thus supplied with a rotating movement, a slag layer protecting the inside walls of the gasification chamber is produced.

However, the invention is not limited to the embodiments described above, but can be varied in many ways within the scope of the following claims. For example, during the gas generation, additional external heat energy can be supplied, for example by preheating the oxidizing agent. For example, in the method according to the present invention, starting material containing carbon and/or hydrogen carbon can be used, which is available in powder and/or liquid and/or in piece form, e.g. coke. For example, additional oxidizing agent can be introduced for the reduction gas generation as well as any slag formers and/or sulfur acceptors in the gasification zone rather than the plasma generator. For example, a mixture of piece-shaped, carbon-bearing material and a suitable sulfur acceptor can be used as shaft filler opposite the combustion zone. The generated reduction gas can be freed of sulfur contamination before entering the reduction shaft. The temperature level of the generated reduction gas can, for example, be kept within a range of between 1000 and 1500°C, and the temperature can be regulated to between 700 to 1000°C, preferably 825°C, before introduction into the reduction shaft. The partially recycled, consumed partial flow of the reduction gas from the reduction shaft can be brought to a pressure necessary for the process, for example with the help of at least one compressor. In the device according to the invention, the main feed line (7) will have at least one compressor (8), and the gas generation shaft (11) will have a draining device (13, 14) for slag.

For example, with the method according to the invention, the gasification zone can be formed in the lower part of a shaft filled with lumpy, solid material. The recycled sub-flow of the shaft gas can be heated if necessary using a heat exchanger in the top gas line.

Claims (29)

1. Method for reduction of oxide-containing material, characterized by a/ that a reducing gas mainly containing carbon oxide and hydrogen gas is produced from starting material containing carbon and/or hydrogen carbon, whereby said starting material together with oxidizing agent and any slag formers is introduced into a gasification zone or a gasification chamber with the simultaneous supply of heat energy from at least one plasma generator ; b/ that the reducing gas produced in this way is brought to a temperature suitable for the subsequent reduction and then introduced into a shaft furnace containing the oxide-containing material intended for reduction and thereby made to flow countercurrently to said material intended for reduction; c) that after the reduction of the oxide-containing material with oxidizing components, such as preferably carbon dioxide and water, as well as dust-like particles, the reducing gas contaminated and thus partially consumed with regard to its reducing power is mainly freed from water and dust-like particles and then mainly returned to the process; d/ that at least a smaller partial flow m of the said, partially consumed and calculated for reuse in the process gas in and before a pressure regulation of the total gas flow is withdrawn from the system and e/ that at least a smaller partial flow of said, partially consumed and calculated for reuse in the process gas before adjusting the f^/CO ratio in the finished reducing gas is made to pass a CG^ scrubber. 2. Method according to claim 1, characterized in that the gas stream used for pressure regulation is flared or reversed for external purposes. 3. Method according to claims 1 and 2, characterized in that the gas stream is withdrawn after the gas emerging from the reduction step has been freed from water vapor and dust-like contaminants. 4. Method according to claims 1-3, characterized in that oxygen gas and/or water and/or recycled gas is used as an oxidizing agent during the gas generation, which is supplied to the gasification zone in whole or in part through the plasma generator. 5. Method according to claim 4, characterized in that said oxidizer added to the plasma generator is preheated before it is introduced into the plasma generator. 6. Method according to claims 1 to 5, characterized in that water or a partial flow of the partially consumed reducing gas is introduced into the shaft filled with piece-shaped reducing material above and at a suitable distance from the gasification zone, so that the surplus heat in the shaft filling is utilized for to convert f^ O to H ? + CO respectively carbon dioxide to carbon monoxide. 7. Method according to claims 1 to 6, characterized in that immediately before the plasma generator, powdered carbon-bearing material is injected as well as any sulfur acceptors and/or slag formers using water or steam or a carrier gas consisting of a partial flow m of the partially consumed, from the reduction shaft removed reducing gas or oxygen gas or air. 8. Method according to one or more of claims 1 to 7, characterized in that the carbon-bearing starting material required for the generation of the reduction gas is introduced into the gasification zone immediately before the plasma generator. 9. Method according to one or more of claims 1 to 8, characterized in that the reduction gas generated in the gasification zone before the introduction of the reduction gas into the reduction shaft is partially freed from any sulfur contamination. 10. Method according to one or more of the preceding claims, characterized in that the temperature of the hot reducing gas exiting the gas generator may be after a s <y> purification a) through mixing with such a quantity of the partially consumed reduction gas withdrawn from the reduction shaft and/or b) by being subjected to a cooling and/or c) by adding such an amount of water and/or steam that the final temperature of the gas is between 700-1000°C. 11. Procedure according to one or more of the preceding requirements, characterized in that the partial flow of recycled shaft gas calculated for temperature control of the reducing gas is heated when needed, i.e. in the case of a large partial gas flow, before it is added to the reducing gas. 12. Procedure according to one or more of the preceding requirements, characterized in that the partial stream of recycled shaft gas used for temperature regulation of the reducing gas formed in the gas generation shaft is regulated with regard to its CC^ content before mixing into the reducing gas. 13. Method according to claims 1 to 12, characterized in that the partially recycled, consumed partial flow of the reduction gas from the reduction shaft is brought to a pressure necessary for the process, for example with the help of at least one compressor. 14. Method according to one or more of claims 1-13, characterized in that to control the "carburization potential" of the reducing gas and to counteract methanation, a carbon carrier, such as methane, methanol and/or propane, is added. 15. Method according to one or more of the preceding claims, characterized in that to counteract soot formation, h^ S is added. 16. Method according to one or more of claims 1-15, characterized in that a two-stage gasification is used for the gas generation of the reducing gas, whereby the starting material is partially combusted and at least partially gasified in the gasification chamber and that the resulting mixture is introduced into a shaft at a bed of piece-shaped, carbonaceous material, whereby the physical heat content of the mixture obtained from the gasification chamber is utilized to reduce the content of carbon dioxide and water in the gas in the coke bed and that the gas generation process is controlled so that the outgoing gas exhibits a temperature and a composition that is adapted to subsequent process steps. 17. Device for reduction of oxide-containing material for carrying out the method according to claim 1, characterized by a generation device for reduction gas which contains a reaction chamber (11), at least one plasma generator (10) opening into the reaction chamber (11), one for the gas generation device (11) ) possibly via a sulfur filter (22) connected to a shaft furnace (1) which contains the oxide-containing material intended for reduction, a gas discharge (4) arranged in the upper part of the shaft furnace (1) and a separator (5) located in connection with the gas discharge (4) ) arranged to free the gas stream from water and dusty particles as well as a subsequent gas discharge (6) calculated for pressure regulation and a main feed line (7) for recirculation of the main gas stream to the gas generation device (11) and/or temperature control of it in the gas generation device ( 11) produced reducing gas. 18. Device according to claim 17, characterized in that the main feeder line (7) has at least one compressor (8). 19. Device according to claims 17 and 18, characterized in that the main feeder line (7) is connected to a CG^ gas scrubber (23). 20. Device according to claim 19, characterized in that the CC^ gas scrubber (23) is equipped with a "bypass" line (7a), which partly ends in a direct extension of the main feeder line (7) for supplying return gas to the gas generation device (11) and partly passes into another main feed line (14) designed to feed carbon dioxide-regulating return gas to, in and before temperature control, calculated mixing in the newly generated reducing gas. 21. Device according to claims 17-20, characterized in that the main feeder line (7) via the "bypass" line (7a) and a first branch line (16) is connected to the upper part of the generation shaft (11). 22. Device according to claims 17-21, characterized in that the main feeder line (7) via the "bypass" line (7a) and another branch line (15) is connected to the reaction zone present in the lower part of the gas generation shaft (11). 23. Device according to claims 17-22, characterized in that the plasma generator (10) is connected to an oxidizing agent supply device for direct passage of this, possibly preheated, oxidizing agent through the plasma generator and to the reaction zone. 24. Device according to one or more of claims 17-23, characterized in that the gas feeder line between the gas generation shaft (11) and the sulfur filter (22) can be connected to a partial flow of return gas via a line (14) and a branch line (17) . 25. Device according to one or more of claims 17-24, characterized in that the reduction gas line between the sulfur separator (22) and the gas inlet (3) of the reduction shaft (1) can be connected to a temperature-regulating partial flow of the gas from line (14) via a cooling device in the form of a mixing chamber (20). 26. Device according to claim 25, characterized in that heating of the partial gas flow of return gas in the mixing chamber (20) is achieved by means of a heat exchanger in the top gas line (4). 27. Device according to one or more of claims 17 to 26, characterized in that a supply device (24) for water and/or steam opens into the supply line (21). 28. Device according to one or more of claims 17 to 27, characterized in that a supply line (25) for a carbon carrier, for example methane, propane and/or methanol opens into the feed line (21). 29. Device according to one or more of claims 17 to 28, characterized in that a supply line (26) for f^ S opens into the feed line (21).