DD229426A5 - METHOD AND DEVICE FOR REDUCING OXIDIC MATERIAL - Google Patents

Abstract

The invention relates to a reduction gas consisting mainly of carbon monoxide and hydrogen, which is produced from carbonaceous or hydrogen-containing material in a special schachtfoermigen gas generator by means of heat energy from at least one plasma generator. The reducing gas thus prepared is, optionally after desulfurization and after adjusting its temperature, introduced into a reduction shaft furnace containing the oxidic material. The partially consumed reducing gas, which is removed from the shaft furnace, is freed of water and dust-like particles, whereupon a partial flow of the recycle gas is supplied to the process again and a smaller partial flow for pressure control in the system is used. A small partial flow of the gas to be recirculated to the process is passed through a CO2 scrubber and then used to adjust the H2 / CO ratio in the finished reducing gas. Fig. 1

Description

Field of the Invention '

The invention relates to a method for the reduction of oxidic material and to a device for carrying out the method.

Characteristic of the known technical solutions

There is no further details as to how the reduction of oxidic material using reduction shaft furnaces has hitherto been carried out.

Object of the invention

The aim of the invention is to provide an optimal method for the reduction of oxidic material.

Explanation of the essence of the invention

The invention has for its object to form the Pozeßtechnologie so that the process is optimized in terms of energy production, in particular to provide an easily controllable gas generating system and to make the process so flexible that the main part of the reducing gas originally used for the reduction of the oxidic material can be used again to produce fresh reducing gas. The process according to the invention for the reduction of oxidic material is characterized essentially by the fact that

a) a reducing gas consisting primarily of carbon monoxide and hydrogen is prepared from a carbonaceous and / or hydrocarbonaceous starting material, this starting material is introduced together with an oxidizing agent and optionally also a slag forming in a gasification zone or a gasification chamber while simultaneously supplying heat energy from at least one plasma generator becomes;

b) the reducing gas thus prepared is brought to a temperature suitable for the subsequent reduction process and then introduced into a reduction shaft furnace containing the oxidic material to be reduced, this gas being passed in countercurrent to the oxidic material;

c) removing substantially all of the water and dust-like particles from the reducing and partially oxidizing constituents such as carbon dioxide and water and dust-like particles after reduction of the oxidic material in terms of reducing ability, and recycling substantially the same;

d) at least a small partial flow of intended for recycling in the process, partially used gas for pressure control of the entire gas stream is withdrawn from the System ^, and

e) at least a small partial stream of intended for recycling in the process, partially spent gas for the purpose of adjusting the H ₂ / CO ratio in the finished gas is passed through a CO ₂ scrubber.

Appropriately, the pressure control is carried out in the system by a small gas delivery. The discharged for pressure control gas flow is expediently flared or otherwise exploited, z. For drying the carbonaceous material used in the process.

Preferably, the gas stream is discharged after the gas leaving the reduction stage has been at least partially freed from water vapor and / or dust-like particles.

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

Preferably, the carbonaceous and / or hydrocarbonaceous starting material is used to produce the reducing gas in powder and / or liquid form and / or particulate form.

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 particulate form, coke being preferably used as the filling.

According to the invention, a partial flow of the partially spent gas containing CO ₂ / taken from the reduction shaft furnace and introduced into the lumpy reducing material filled gas generator from above and at a suitable distance from the combustion zone to take advantage of the heat in the pit filling to H ₂ O in H ₂ + CO and convert the carbon dioxide into carbon monoxide. A partial flow of this recycle stream of spent reducing gas from the shaft furnace may also be used as a carrier gas for the introduction of a powdered carbonaceous material and / or a slag former together optionally with sulfur acceptors immediately prior to the plasma generator.

A partial flow of this recycle stream of spent reducing gas from the shaft furnace is also used as a carrier gas for the thermal energy supplied by the plasma generator.

Preferably, the CO ₂ content of the recycle gas to be recirculated to the process is adjusted by passing a desired amount of recycle gas through a CO ₂ scrubber.

Conveniently, the reducing gas produced in the gas generator is freed of any sulfur contaminants by introducing suitable sulfur acceptors into the well fill and / or by passing the withdrawn gas through a sulfur filter. Alternatively, sulfur acceptors can also be blown into the gasification zone.

According to another proposal of the invention, the temperature of the reducing gas taken 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 reduction gas from the reduction shaft furnace and / or

b) is subjected to cooling and / or

c) it is added to such an amount of water and / or water vapor that the desired temperature is reached.

When only a small amount of this partially spent reducing gas is used for temperature control, this partially spent reducing gas is cooled as it passes through the gas scrubber located immediately behind the gas outlet from the top of the reduction shaft furnace so that the desired final gas mixture temperature is readily achievable. However, if a strong reflux is mixed with the freshly generated reducing gas, this reflux is conveniently preheated prior to mixing with the reducing agent using, for example, a placer solvent

Preferably, the CO ₂ content of the partial stream used for temperature control of the reducing gas generated in the gas generator is adjusted to recycled top gas before this partial stream is mixed with the reducing gas.

Furthermore, H ₂ S may be added to the final reducing gas to prevent soot build-up.

Preferably, the reducing gas is produced by means of a two-stage gasification in which the starting material is partially combusted and at least partially gasified in a gasification chamber, whereupon this gas mixture is introduced into a shaft containing a bed of carbonaceous particulate material and the physical heat content of the mixture of the Gasification chamber is exploited in the bed of carbonaceous lumpy material to reduce the content of carbon dioxide and water in the gas, wherein the gas generating process is controlled so that the withdrawn gas has a suitable temperature and composition for a subsequent process step.

A device according to the invention for the reduction of oxidic material with simultaneous production of a suitable reflux or circulation 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 the mouth lying in the bottom of the reaction chamber, one to the gas generator optionally connected via a sulfur filter shaft furnace containing the oxidizing material to be reduced, arranged in the upper part of this shaft furnace gas outlet, arranged next to this gas outlet separator for water and dust-like particles from the exiting gas stream and a subsequent gas outlet for pressure control and a main return line for the Main part of this gas to the gas generator, and optionally via a CO ₂ scrubber.

In the main return line expediently at least one compressor is turned on.

Conveniently, the main return line is connected to a CO ₂ scrubber. The CGy scrubber preferably has a secondary line which opens into a direct extension of the main line for feeding circulating gas into the gas generator and also into a second main line via which practically CO ₂ -free circulating gas is mixed with the freshly generated reducing gas for temperature control.

The second main return line is connected via the secondary line and a first branch line to the upper region of the gas generator.

In a particular embodiment, the main return line is connected via the secondary line and a second branch line to the reaction zone in the lower part of the gas generator.

The plasma generator is connected to a supply of oxidant for the direct passage of the optionally preheated oxidant through the plasma generator into the reaction zone.

The gas generator has a slag outlet. The gas generator receives a bed of carbonaceous particulate material, optionally with sulfur acceptors.

The gas line between the gas generator and the sulfur filter can be connected via a pipeline and a branch line to a partial flow of circulating gas.

The reducing gas line between the sulfur separator and the gas inlet of the reduction shaft furnace with a temperature-regulating partial gas flow is connectable via a cooling device in the form of a mixing chamber.

For heating the partial flow of recirculated gas in the mixing chamber, heat exchangers are arranged in the top gas return line.

In the feed line opens a supply line for water vapor. Furthermore, opens into the feed line a supply line for a.Kohlenstoffträger, z. As a methane, propane and / or methanol, as well as a supply line for H ₂ S.

embodiment

The invention will be explained in more detail in two subsequent examples and further features and features highlighted.

The accompanying drawings show:

1 shows a schematic representation of a device according to the invention with a single-stage gas generator; and FIG. 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 FIG. 1 has a reduction shaft furnace 1 for the reduction of oxidic, lumpy material. This shaft furnace 1 has a charging device 2 for introducing oxidic, lumpy material to be reduced. At the bottom of the shaft furnace 1 is an inlet line 3 for hot reducing gas, which consists essentially of carbon monoxide and hydrogen, said gas is passed in countercurrent through the shaft furnace 1. The outlet conduit 4 is connected to a dust-like particle separator 5 and water, a so-called gas scrubber, from which the gas freed of water and dust particles and simultaneously cooled flows to an outlet 6 provided for pressure control and then through a main return conduit 7 for re-use in the process is returned, as will be described later. The main return line 7 includes a compressor 8.

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

Behind the compressor 8, the return line 7 is connected to a CO ₂ scrubber 23. This arrangement also has a secondary line 7a, which opens into a direct extension of leading to the gas generator 11 return line 7 for circulating gas. It also flows into a second main return line 14 for circulating gas, but this second line 14 of CO ₂ supplies virtually free circulating gas to the freshly generated reducing gas for its temperature control. In principle, this arrangement offers the following functional conveniences:

Via a first branch line 16, the line 14 can be connected to the upper region of the gas generator 11; the main return line 7 can be connected via additional branch lines 15 and 15a with the gasification zone in the lower region of the gas generator 11, d. h., circulating gas can be fed before the plasma generator 10 through the line 15 and after compression in the compressor 8a via the line 15a behind the plasma generator 10 to go through this:

Via a further branch line 17, the line 14 with the removed from the gas generator 11 reducing gas, which leaves the upper part of the gas generator 11 via an outlet 18, are connected, and via a further branch line 19, the conduit 14 via a mixing chamber 20 with the Finally, the line 14 may be connected to the reducing gas line 21 immediately before the entry of the reducing gas into the reduction shaft furnace 1, and the line 14 may be connected to a sulfur filter 22 via a reducing gas.

In this way, the CO ₂ content in the circulation gas can be controlled properly.

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 connected directly to the plasma generator 10, optionally after preheating, whereby this oxidizing agent is fed to the reaction zone in the bottom of the gas generator 11 can.

The above and in FIg. 1 device operates in principle as follows:

The reducing gas for the reduction of the oxidic material in the shaft furnace 1, which is introduced into the same via the inlet conduit 3, is generated in principle in the gas generator 11 by a carbonaceous and / or hydrocarbon-containing starting material together with oxidizing agent and optionally with slag forming a gasification zone in the lower part of Gas generator 11 is supplied while heat energy is added via at least one Pfaffenager 10 at the same time. The reducing gas produced in this way is then brought in principle to a suitable for the subsequent reduction of the oxidic material in the shaft furnace 1 temperature and injected into the shaft furnace 1 in countercurrent to the material to be reduced. After reduction of the oxide material, the reducing gas contains oxidizing components such as carbon dioxide and water and dust-like particles, and is therefore partially consumed in its reducing ability. The reducing gas is withdrawn through the gas outlet line 4 from the gout of the reduction shaft furnace 1 and then freed of water and dust-like particles in the gas scrubber 5. A small portion of the gas thus treated in the gas scrubber 5, which has been simultaneously cooled, is then withdrawn from the system via the gas outlet conduit 6 for temperature control, while the main stream of this gas is recycled to the process through the return conduit 7, d. H. it can be used again to generate reducing gas.

The gas generation in the shaft-shaped gas generator 11 can be achieved in various ways. Powdery and / or liquid carbonaceous and / or hydrocarbonaceous starting material may be introduced into the gasification zone, for example by a supply line 12; 13, in which case oxidizing agents such as, for example, oxygen or water vapor can be introduced into the reaction zone through the plasma generator 10. Recirculating gas may be supplied to the reaction zone upstream of the plasma torch via line 15, or the gas may be supplied through plasma generator 10 via line 15a. The carbonaceous and / or hydrocarbonaceous starting material may also be supplied in particulate form via the gout of the gas generator 11, so that the gasification zone is formed in the lower part of the gas generator 11 filled with solid carbonaceous material in particulate form. Conveniently, 11 coke is used as a carbonaceous filling of the gas generator.

In addition, water or a part of the partially consumed reducing gas, which has been withdrawn from the reduction shaft furnace 1 via the line 7 and the branch line 16, may 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 through the gasification zone itself and at a suitable distance from it, exploiting the heat of the pit filling to convert H ₂ O to H ₂ + CO and carbon dioxide to carbon monoxide.

The generation of gas in the gas generator 11 can also be achieved by injecting pulverulent, carbonaceous material, optionally with sulfur acceptors and / or slag formers, by means of steam or a carrier gas which consists of partially consumed reducing gas of a substream taken from the reduction shaft furnace 1, or oxygen or a mixture of oxygen and water vapor.

The reducing gas generated in the gas generator 11 may be desulfurized by, for example, adding a suitable sulfur acceptor to the pit charge, or by injecting sulfur acceptors into the gasification zone, or by passing the gas generated in the gas generator 11 through the discharge conduit 18 to a sulfur separation filter 22. Any remaining sulfur impurities are absorbed by the metal oxide reduced in the lower part of the reduction shaft furnace 1.

The reducing gas is generally maintained at a temperature range of 1000 to 1500 ° C. However, such a hot reducing gas can not be used directly for reduction in the reduction shaft furnace 1, so that a temperature must be lowered before being introduced into the shaft furnace 1. This can be done in various ways within the scope of the invention.

For example, the reducing gas flowing out of the gas generator 11 can be mixed via line 18 with a suitable partial flow of circulating gas. This is done via line 14, so that the temperature of the gas mixture is between 700 and 1000 ⁰ C. Alternatively, this mixing with a partial stream of the gas recirculated from the reduction shaft furnace 1 can be achieved by mixing the reducing gas 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 recycle gas from the line is used, this should be sufficient to effect the desired cooling of the generated reducing gas. However, if an excessively large amount of circulating gas is added to the reducing gas, such a strong flow should preferably be heated to the exact temperature in the mixing chamber 20. This heating can be done for example by means of a plasma generator.

The temperature setting can also be achieved by passing a partial flow of the gas produced through lines 21 and 19 through a mixing chamber 20 acting as a cooler.

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

In order to control the carburizing potential of the generated reducing gas and to prevent methanation, suitable carbonaceous materials such as methane, methanol and / or propane may be supplied via line 25.

Soot deposits can also be counteracted by H ₂ S being blown in via line 26.

An important feature of the invention is that the CO ₂ content in the recycle gas used to control the temperature of the reducing gas can be continuously controlled by the CO ₂ scrubber.

The above-described generation of reducing gas in the shaft-like gas generator 11 can also be performed by a two-stage gasification, as shown in FIG.

The gas generation according to the invention offers important technical advantages. Gas generation may be carried out at temperatures such that the ash forms an easily handled slag, which is discharged without causing clogging problems in the process. The hydrogen content in the reduction gas may be controlled to a percentage suitable for the reduction process by controlled blowing of water and / or oxygen in the gas generation stage and in the temperature control stage. Also in terms of energy consumption, an optimal reduction process and a conveniently controllable gas generating system is realized. The control of the proportions of H ₂ O and CO ₂ in the line 3 can consequently be carried out in such a way that the flow in the lines 14 to 18 and 21 to 3 and also in the line 24 is adjusted.

As already mentioned, the desulphurisation can also be installed directly in the gas generator instead of by means of a special sulfur filter, for example by providing the coke bed with suitable material or by blowing suitable material into the gasification zone.

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

2 has a gasification chamber 29 and a shaft 30 filled with a coke bed.

The gasification chamber 29 has a water-cooled outer shell 32 and a refractory lining 33 and is preferably formed 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 particulate form is fed to the shaft 30 through a gas-tight feed 36 at the top. The mouth of the gasification chamber 29 is located in the lower part of the shaft 30, and the gas flows through the coke bed upwards and out of the shaft 30 through the gas outlet 35. In the illustrated embodiment, the slag outlet 34 is used for the gasification chamber 29 and the shaft 30 together. In connection with the gasification chamber 29 at least one burner is provided, which consists of a plasma generator 37 in the illustrated Auführungsbeispiel. The plasma generator 37 is connected to the gasification chamber 29 through a valve 38. Oxidizing agent is passed into the plasma generator 37 through a feed line 9 or can also be introduced in front of the plasma generator 37 through a feed line 39. The oxidizing agent may also consist of a carrier gas, which is passed through the plasma generator 37, or from a circulating gas, which is supplied through the line 15 a. The hot turbulent gas which is generated in the plasma generator 37 passes through the mouth 40 of the plasma generator 37 into the gasification chamber 29. The carbonaceous fuel, preferably in powder form, is injected through a feed line 41 into an annular space 42 concentrically around the mouth of the Plasma generator 37 is formed, and / or by a lance 43, which can also be used for the supply of additional charges such as slag.

In the shaft 30 also lances 44 and 45 are provided, through which optional further oxidizing agent such as H ₂ O, CO ₂ , can be added to take advantage of the physical excess heat in the gas. This also allows the temperature and composition of the gas to be controlled.

At the outlet of the gasification chamber 29, a first sensor 46 is arranged, while a second sensor 47 in the gas outlet 35 of the shaft 30 is seated. These sensors 46; 47 are used to measure the temperature and / or analysis of the gas. These two sensors 46; 47 give the opportunity to control the process by controlling the supplied external energy and / or the supplied material streams.

2 shows only one embodiment of a suitable two-stage gas generator 31 in a plant for carrying out the method according to the invention, with many other solutions are also conceivable. For example, the plasma generators 37 can be arranged tangentially on the circumference of the gasification chamber 29, so that in the gasification chamber 29, a circulating flow is achieved. In addition, to facilitate slag separation, the gasification chamber 29 may be arranged vertically, or the gasification chamber 29 and the well 30 may be provided with separate slag outlets 34.

2, the starting material is partially burned and at least partially gasified in the gasification chamber 29, and the mixture thus obtained is introduced into a shaft 30 containing a bed of carbonaceous material in particulate form. The physical heat content of the gas mixture exiting the gasification chamber 29 is thereby utilized in the coke bed to reduce the content of carbon dioxide and water in the gas. In this way, the gas generating process can be controlled so that the outflowing gas has a readily compatible with the subsequent process step temperature and context. The carrier gas coming from the plasma generator 37 expediently receives a rotational movement before it is introduced into the gasification chamber 29, and the powdery carbonaceous fuel can be introduced concentrically around the hot gas stream which flows into the gasification chamber 29. Characterized in that the material in the gasification chamber 29 receives a rotational movement, there is a protective layer of slag on the inner walls of the gasification chamber 29th

Naturally, the invention is by no means intended to the above-described embodiments, but can be modified in many ways. For example, to generate gas by preheating the oxidant from the outside heat energy can be supplied.

Claims (39)

Invention claim: 1. A process for the reduction of oxidic material, characterized in that a) a reducing gas consisting primarily of carbon monoxide and hydrogen is prepared from a carbonaceous and / or hydrocarbonaceous starting material, said starting material together with an oxidizing agent and optionally also a slag forming agent in a gasification zone or a gasification chamber (29) is introduced, while at the same heat energy of at least a plasma generator (10, 37) is supplied; b) the reducing gas thus prepared is brought to a temperature suitable for the subsequent reduction process and then introduced into a reduction shaft furnace (1) containing the oxidic material to be reduced, this gas being passed in countercurrent to the oxidic material; c) removing substantially all of the water and dust-like particles from the reducing and partly oxidizing constituents such as carbon dioxide and water and dust-like particles after reduction of the oxidic material and substantially returning it to the process; d) at least a small partial stream of provided for recycling in the process, partially used gas for pressure control of the entire gas stream is withdrawn from the system; and e) at least a small partial stream of intended for recycling in the process, partially spent gas for the purpose of adjusting the H ₂ / CO ratio in the finished gas by a CO ₂ scrubber (23) is passed. 2. The method according to item 1, characterized in that the gas stream withdrawn for pressure control flared or consumed for external purposes. 3. The method according to item 1 or 2, characterized in that the gas stream is withdrawn after the gas leaving the reduction stage was freed of water and dust-like particles. 4. The method according to item 1, characterized in that oxygen and / or water and / or circulating gas is used as the oxidizing agent for the gas production and the gasification zone is supplied in whole or in part by the plasma generator (10) 37). 5. Method according to item 4, characterized in that the oxidizing agent supplied by the plasma generator (10; 37) is preheated before it enters the plasma generator (10; 37). 6. The method according to any of items 1 to 5, characterized in that the carbonaceous and / or hydrocarbonaceous starting material for producing the reducing gas in powder form and / or liquid form and / or particulate form is used. A method according to any one of items 1 to 6, characterized in that the gasification zone is formed in the lower portion of a shaft-shaped inflator (11; 31) filled with solid carbonaceous material in particulate form. 8. The method according to item 7, characterized in that coke is used as the carbonaceous filling of the shaft (11; A method according to any one of items 1 to 8, characterized in that water or a partial flow of the partially spent reducing gas is introduced into the reducing furnace in lump form filled shaft furnace (1) above and at a suitable distance from the gasification zone to heat exploiting in the pit filling for the conversion of H ₂ O in H ₂ + CO and the carbon dioxide in carbon monoxide. 10. The method according to any one of items 1 to 9, characterized in that powdered carbonaceous material and / or slag forming agent, optionally together with sulfur acceptors, injected into the system immediately before the plasma generator (10, 37) by means of water or steam or a carrier gas which consists of a partial flow of the partially spent reducing gas which has been withdrawn from the reduction shaft furnace (1), or of oxygen or air. 11. The method according to any one of items 1 to 10, characterized in that the carbonaceous starting material required to generate the reducing gas is introduced into the gasification zone immediately before the plasma generator (10, 37). 12. The method according to any one of items 1 to 11, characterized in that optionally additional oxidizing agent for generating the reducing gas and optionally also slag formers and / or sulfur acceptors in the gasification zone in front of the plasma generator (10; 37) are introduced. A process according to any one of items 1 to 12, characterized in that a mixture of carbonaceous particulate material and a suitable sulfur acceptor is used as the well fill above the gasification zone. A process according to any one of items 1 to 13, characterized in that the reducing gas produced in the gasification zone is desulphurized before being introduced into the reduction shaft furnace (1). < 15. The method according to any one of items 1 to 14, characterized in that the freshly generated reducing gas has a temperature between 1000 and 1500 ^c C. A method according to any one of items 1 to 15, characterized in that the temperature of the generated reducing gas is controlled to 700 to 1,000 ° C, preferably 825 ° C, before being introduced into the reduction shaft furnace (1). - - 17. The method according to item 16, characterized in that the temperature of the gas generator (11, 31) leaving the hot reducing gas is possibly controlled by its desulfurization by a) such an amount of the partially consumed reducing gas, which was taken from the reduction shaft furnace (1) is admixed 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 final temperature of the gas is between 700 and 1000 ° C. 18. The method according to any one of the preceding points, characterized in that a large partial flow is heated to re-circulated top gas of the reduction shaft furnace (1) for the purpose of controlling the temperature of the reducing gas before its addition to the reducing gas, if necessary. 19. The method according to item 18, characterized in that the heating by means of heat exchangers (20) is carried out in the top gas supply line. A method according to any one of the preceding claims, characterized in that the substream is recycled to re-circulated top gas which is used to control the temperature of the reducing gas produced in the gas generator (11; 31) before mixing with the reducing gas with respect to its CO ₂ Content is adjusted. 21. The method according to any one of items 1 to 20, characterized in that the recirculated partial flow of spent reducing gas from the reduction shaft furnace (1) by means of at least one compressor (8) is brought to the pressure required for the process. 22. The method according to any one of items 1 to 21, characterized in that a carbon carrier such as methane, methanol and / or propane is added to control the carburizing potential of the generated reducing gas and to counteract methanation. 23. The method according to any one of the items 1 to 22, characterized in that H ₂ S is supplied as an antidote to soot deposits. 24. The method according to any one of the items 1 to 23, characterized in that the reducing gas by means of a two-stage. Gasification is generated in which the starting material is partially burned and at least partially gasified in a gasification chamber (29), whereupon the gas mixture thus obtained in a bed of carbonaceous, particulate material containing shaft (31) is introduced and that the physical heat content of the mixture from the gasification chamber (29) in the bed of carbonaceous particulate material to reduce the content of carbon dioxide and water in the gas, the gas generating process being controlled so that the withdrawn gas has a temperature and composition suitable for a subsequent process step , 25. A device for the reduction of oxidic material for carrying out the method according to item 1, characterized by a gas generator (11, 31) for reducing gas with a reaction chamber, at least one plasma generator (10, 37) with in the bottom of the reaction chamber lying mouth, one to the Gas generator (11; 31) optionally via a sulfur filter (22) connected shaft furnace (1) containing the oxidic material to be reduced, arranged in the upper part of this shaft furnace gas outlet (4), a next to this gas outlet (4) arranged separator (5 ) for separating water and dust-like particles from the gas stream and a subsequent gas outlet (6) for pressure control and a main return line (7; 14) for the main gas flow to the gas generator (11; 31) and / or for temperature control of the in the gas generator (11; ) generated reducing gas. 26. Device according to item 25, characterized in that the main return line (7; 14) is provided with at least one compressor (8). 27. Device according to item 25 or 26, characterized in that the main return line (7; 14) to a COyWäscher (23) is connected. 28. The device according to item 27, characterized in that the COyWäscher (23) with a secondary line (7 a) is provided, which in a direct extension of the gas generator (11; 31) leading main return line (7) and also in a second main line (14) opens, via which the circulating gas whose CO ₂ content has been set, with the newly generated reducing gas for temperature control of the same is miscible. Device according to any one of items 25 to 28, characterized in that the second main return line (14) is connected to the upper part of the gas generator (11; 31) via the secondary line (17) and a first branch line (18). Device according to any one of items 25 to 29, characterized in that the main return line (7) is connected via the secondary line (15a) and a second branch line (15) to the reaction zone in the lower part of the gas generator (11; Apparatus according to any one of items 25 to 30, characterized in that the plasma generator (10; 37) is connected to a supply of oxidants for the direct passage of the optionally preheated oxidant through the plasma generator into the reaction zone. 32. Device according to any one of items 26 to 31, characterized in that the gas generator (11; 31) has a slag outlet (13; 34). 33. Device according to any one of items 26 to 32, characterized in that the gas generator (11; 31) receives a bed of carbonaceous particulate material, optionally with sulfur acceptors. 34. Device according to any one of items 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 of circulating gas can be connected. 35. Device according to any one of items 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 via a cooling device in the form of a mixing chamber (20) is connectable. 36. Device according to item 35, characterized in that for heating the partial flow to recirculated gas in the mixing chamber (20) heat exchangers are arranged in the top gas return line. 37. Device according to any one of items 25 to 36, characterized in that in the feed line (3) has a supply line (24) opens for water vapor. 38. Device according to any one of items 25 to 37, characterized in that a supply line (25) for a carbon carrier, for. As methane, propane and / or methanol, in the feed line (3) opens. 39. Device according to any one of items 25 to 28, characterized in that a supply line (26) for H ₂ S opens into the feed line (3). For this 2 pages drawings