RU2136763C1 - Method of direct reduction of fine-grained material containing iron oxide in form of particles and plant for method embodiment - Google Patents

Abstract

FIELD: metallurgy. SUBSTANCE: in direct reduction of material containing iron oxide in form of particles in fluidized bed, reformed gas purified, at least, partially from CO₂, in capacity of reducing gas is brought to reducing zone with fluidized bed and withdrawn from bed in form of top gas. The latter is used, at least, partially in mixture with reformed gas for direct reduction. For the purpose of means saving, in units operating with reducing gas, and for saving of expenditures for heating, at least, 50-100% of reformed gas and from 0 to 100% of top gas are purified from, at least, partially from CH₄ and N₂ by adsorption, in addition to carbon dioxide gas. Effluent gas separated from reformed or top gas by adsorption is used as fuel gas. EFFECT: reduced power of adsorption device of varying pressure and reduced expenditures for heating with invariable or increased production efficiency. 14 cl, 2 dwg, 3 tbl

Description

The invention relates to a method for the direct reduction of an iron oxide-containing material in the form of particles in a fluidized bed, wherein the reformed gas, purified at least partially from CO ₂ , is supplied as a reducing gas to the recovery zone with a fluidized bed and discharged from it in the form of top gas, and wherein the top gas is applied at least partially in conjunction with the reformed gas for direct reduction, as well as to the installation for implementing this method.

 A method of this type is known from EP-A-0571358 and US-A-5,082,251. At the same time, iron-rich ore fines are recovered in a system of successive fluidized bed reactors using reducing gas obtained from natural gas by reforming under elevated pressure. The powdered iron obtained in this process is then subjected to hot or cold briquetting.

In these known methods, in order to avoid too high a CO ₂ content in the reducing gas, CO _{2 is} removed from the reducing gas before it enters the first fluidized bed reactor by flushing using a conventional CO ₂ flushing based on the principle of physical or chemical absorption. Due to washing with CO ₂ , very high selectivity is achieved, that is, CO ₂ and H ₂ S are removed from the gas stream being cleaned. Other molecules, for example, H ₂ , CH ₄ , N ₂ , etc., practically do not bind absorbent and remain in the cleaned gas stream. Natural gas is used to heat the reformer and, in addition, to heat the reducing gas heater, with top gas being added, if necessary.

The objective of the invention is to further improve these known methods, namely in the sense that while maintaining the reducing ability to reduce the volume of reducing gas than to save in those units of the installation that work with reducing gas. So, in particular, it is necessary to achieve savings in investment costs for compressors for reducing gas and a decrease in the energy consumption for compression of the reducing gas, as well as a decrease in heating costs, however, the productivity should at least remain unchanged or increase. In addition, the exhaust gas obtained in the CO ₂ purification plant must be used in the process itself.

This problem in the method of the above type is solved due to the fact that from 50-100% of the reformable gas and 0-100% of the top gas by absorption, in addition to CO ₂ , at least partially, CH ₄ and N ₂ are removed, preferably by adsorption under variable pressure, that the reducing gas is heated, and that the exhaust gas removed by adsorption from the reformed gas or blast furnace gas is used as combustible gas. From DE - C - 4037977 it is known that for direct reduction of lumpy iron ore for direct reduction, a scrubber for washing with CO ₂ or a unit for adsorption with variable pressure is optionally used. At the same time, lumpy iron ore is restored in the reduction shaft furnace using a fixed-bed method, and after unloading from the reduction shaft furnace, it is placed in a melting gasifier, in which reducing gas is supplied from coal and oxygen and supplied to the reduction shaft furnace and the reduced iron ore is melted. This is a method carried out at low pressure, while in the method with a fluidized bed according to the invention, the reducing gas is supplied at a significantly higher pressure. This gives a particular advantage according to the invention due to the fact that, in contrast to the known methods, no additional compressors are required to direct the gas to adsorption. Therefore, in the method according to the invention, high energy savings are obtained.

In the adsorption method, in comparison with the washing from CO ₂ , it is possible to reduce the specific volumes of the reducing gas with a constant reducing ability, namely due to the fact that much more CH ₄ and nitrogen N _{2 are} separated during adsorption, compared with the washing from CO ₂ . Due to this, savings are obtained on installation components such as pipes, compressors, valves, etc.

 Since the exhaust gas removed from the reformed gas or blast furnace gas by adsorption by alternating pressure has a very high calorific value, it is advisable to use it for heating the reducing gas and / or as a combustible gas for the reforming process upon receipt of the reformed gas.

It is advisable to cool the reformed gas strongly before removing CO ₂ , if necessary, by mixing with blast furnace gas, preferably to a temperature of 20 - 100 ^o C, in particular from 30 to 50 ^o C, due to which it is possible to significantly increase the efficiency pressure swing adsorption.

 The implementation of the method according to the invention creates an advantage especially when the direct reduction of the iron-containing material in the form of particles is carried out in several recovery zones with a fluidized bed, successively arranged one after another, and the iron-containing material in the form of particles is directed from one zone with a fluidized bed to another zone with a fluidized bed layer under the action of gravity from top to bottom, and the reducing gas is passed from one zone with a fluidized bed to another zone with ps the fluidized bed in the opposite direction, and the reducing gas consumed in the direct recovery is discharged as top gas from the uppermost recovery zone in the fluidized bed, mixed with the reformed gas and used as the reducing gas.

It is advisable if the heating gas is heated in two stages, namely, in the first stage - by heat transfer, and in the second stage - by partial combustion with the help of oxygen introduced into the reducing gas. This has a particular advantage when using a variable pressure adsorption device, since in a variable pressure adsorption device, a reducing gas with a water content of 0% by volume is obtained. Due to this, it is possible to keep the water content in the reducing gas, including after heating by additional combustion or partial burning, at a very low level, although with additional burning or partial burning, the H ₂ O content increases in favor of the H ₂ content by 1-5% vol . The possible loss of CO due to additional or partial combustion can be compensated by changing the reforming mode, for example, a lower steam / carbon ratio or, for example, an increased bypass flow to the adsorption device.

An apparatus for carrying out this method according to the invention with at least one fluidized bed reactor for receiving material containing iron oxide, a conduit for supplying reducing gas to this fluidized bed reactor and a conduit for discharging flue gas generated during reduction from the reactor with a fluidized bed, with a reformer, a reformed gas pipeline extending from the reformer, which has a common outlet with a top gas pipeline, and pheno- gas obtained from reformed gas and top gas via the line for the reducing gas supplied to the fluidized bed reactor, and with the installation for the purification of CO _2, characterized in that the apparatus for purifying CO ₂ is formed as an adsorption device, preferably in the form of an adsorption device with a variable pressure, that the pipeline leading to the gas purified from CO ₂ from the adsorption device to the heating device, and the pipe that discharges the exhaust gas released in the adsorption device Property, go to the heating device.

 To simplify the regulation of the desired chemical composition of the reducing gas, the adsorption device is shunted by a branch pipe for top gas, and, if necessary, a branch pipe for reformed gas, leaving the pipeline with reformed gas.

 It is advisable to connect the pipeline for the removal of exhaust gas with the heating device of the reformer or with a gas heater for reducing gas.

 In order to achieve an optimum efficiency by the adsorption device with variable pressure, it is preferable to arrange a gas cooler in the pipeline for supplying gas to the adsorption device.

 The optimal implementation of the installation according to the invention is characterized in that several fluidized bed reactors are connected in series, one after another, and the material containing iron oxide is fed from one fluidized bed reactor to another fluidized bed reactor in one direction, and the recovery gas is passed from one fluidized bed reactor to another fluidized bed reactor through connecting pipelines in the other direction, with and each fluidized bed reactor cyclones are for precipitation of small particles entrained in a reducing gas.

 Effective heating of the reducing gas is characterized by the fact that as a heating device for the reducing gas there is a heat exchanger and a device connected in series with it for partial combustion of the reducing gas with oxygen supply.

 Below the invention is explained in more detail using two exemplary embodiments shown in the drawings, moreover, schematically in FIG. 1 and 2 show preferred embodiments.

 The installation according to the invention has four series-connected fluidized bed reactors 1 to 4 shown in FIG. 1, and the material containing iron oxide, for example, ore fines, is fed through the ore pipe 5 to the first fluidized bed reactor 1 in which heating to the reduction temperature (or preliminary reduction) takes place, and is then sent via transport pipelines 6 from one fluidized bed reactor to another fluidized bed reactor. The finally reduced material (sponge iron) is briquetted in the hot state in the briquetting device 7. If necessary, the reduced iron is protected by re-oxidation during briquetting by supplying an inert gas, not shown in the drawing.

 Before supplying ore fines to the first fluidized bed reactor 1, ore is prepared, for example, by drying and sieving, which is not explained in more detail.

 The reducing gas is passed in countercurrent to the passage of ore from the fluidized bed reactor 4 to the fluidized bed reactors 3 - 1 and, in the form of blast furnace gas, is discharged through the blast furnace gas line 8 from the latter in the gas flow direction of the fluidized bed reactor 1, and is cooled and it is washed in a scrubber 9. Inside the fluidized bed reactors 1 to 4 there are cyclones not shown in the drawing for separating fine particles entrained by the reducing gas.

The production of reducing gas is carried out by reforming the desulfurized in the device for desulfurization of natural gas supplied through the pipe 11 in the reformer 10. The gas formed from natural gas and steam leaving the reformer 10 consists mainly of H ₂ , CO, CH ₄ , H ₂ O and CO ₂ . This reformed natural gas is piped 13 to several heat exchangers 14 in which it is cooled with condensation of water from the gas.

The reformed gas line 13 enters the top gas discharge line 8 after the gas has been compressed by the compressor 15. The gas mixture thus obtained is passed through an alternating pressure adsorption device 16 and is cleaned of CO ₂ , as well as at least at least partially from H ₂ S, CH ₄ , N ₂ . Now it can be used as reducing gas.

In the adsorption device 16 with the gas accumulator 16 ', the gas to be purified is passed through a container with molecular sieves; depending on the choice of adsorbent, preferably molecules are determined, determined by their size and polarity. In this case, the purification of synthesis gas obtained from natural gas by reforming or recirculating blast furnace gas, the selectivity is less than when washing from CO ₂ , since a greater percentage of the gas being purified is deposited into the sediment. This flue gas, in contrast to the flue gas after flushing from CO ₂ , has a higher calorific value and can therefore be burned in furnaces necessary for the direct reduction process, for example, for heating the reducing gas or heating the steam reformer, and thereby decrease external sources of energy needed for burning.

 The accumulator 16 'for receiving the exhaust gas is connected by a pipe 16' 'to the steam reformer 10 for heating it and with a gas heater 19 for heating the reducing gas.

The variable pressure adsorption device 16 is located in front of the gas cooler 17, in which the gas supplied to the variable pressure adsorption device 16 is cooled to about 40 ^° C. or lower, thereby providing a high efficiency of the variable pressure adsorption device 16. Cooling can be carried out by direct cooling with water or indirect cooling.

This reducing gas is supplied through a reducing gas pipe 18 to a gas heater 19 located behind the variable pressure adsorption device 16, is heated to a temperature of about 800 ^° C. and introduced into the first, in the direction of gas flow, reactor 4 with a fluidized bed, where it reacts - for direct iron production - with ore fines. Fluidized bed reactors 4 to 1 are connected in series; reducing gas through the connecting pipes 20 comes from the reactor 4 with a fluidized bed to the reactors 3, 2 and 1 with a fluidized bed.

 According to the invention, either only reformed gas or a mixture consisting of 50-100% reformed gas and 0-100% top gas is supplied to the variable pressure adsorption device 16.

 A pipe 21 branches off from the reformed gas line 13, namely, before the reformed gas line 13 is connected to the open gas pipe 8. This branch pipe 21 is combined with a reducing gas pipe 18 leading from a variable pressure adsorption device 16 to a gas heater 19. Then, another branch pipe 22, which is also combined with a reducing gas pipe 18 leading from a pipe 8 for discharging top gas, from the adsorption device 16 of variable pressure to the gas heater 19. Using both of these branch pipelines 21, 22, equipped, of course, like all other gas ode, valves, it is possible either to bring the adsorption device 16, the variable pressure only 100% of the reformed gas, or to bring the adsorption device 16, the variable pressure gas mixture from 50-100% of the reformed gas and the top gas of 0-100%.

In order to establish a specific chemical composition of the reducing gas, along with the choice of a special adsorbent, there are the following options:
Particular transmission of partial flows in the range from 0 to 100% of the gases supplied to the variable pressure adsorption device 16, preferably from 0 to 30% of synthesis gas or reformed gas, and so on, or, preferably, from 0 to 100% of recycled top gas .

Based on the fact that the variable pressure adsorption device 16 slots more CH ₄ and N ₂ compared to flushing from CO ₂ , it is possible to reduce the specific volumes of the reducing gas with the same reducing ability. Thanks to this, you can save on the corresponding installation nodes. If a higher CH ₄ content than can be achieved using the above connection options is desired, then natural gas or pure CH ₄ can be fed into the reducing gas stream in conduit 23 fed to the fluidized bed reactors 1 to 4.

Part of the top gas is discharged from the gas circuit 8 in order to prevent an increase in the content of gases, for example, N ₂ . Sluice top gas through a branch pipe is supplied to a gas heater 19 to heat the reducing gas and is burned there. In the event of a lack of energy, it is replenished with natural gas supplied through line 24.

 The tangible heat of the reformed natural gas leaving the reformer 10, as well as the reformed flue gas, is used in the recuperator 25 in order to preheat the natural gas after passing through the desulfurization device 12, to obtain the steam necessary for reforming, and also, if necessary, to heat the recovery gas. The combustion air supplied to the reformer via line 27 is also heated.

 In order to prevent a decrease in temperature in the first - in the direction of ore flow - reactor 1 with a fluidized bed, it may be preferable to burn part of the reducing gas leaving the second reactor 2 with a fluidized bed in the first reactor 1 with a fluidized bed, for which, in the first reactor 1 s the fluidized bed includes a pipe 28 for supplying oxygen and, if necessary, a pipe 29 for supplying natural gas.

 In order to maintain the reaction temperature in all reactors 1–4 with a fluidized bed at the same level and thereby ensure a further reduction in energy demand, hot and fresh reducing gas is introduced directly through the branch pipes 30 directly into reactors 1–3 with a fluidized bed, which are located behind the reactor 4 with a fluidized bed, the first in the direction of flow, namely in an amount of about 10% for each reactor 1, 2, 3 with a fluidized bed. The fluidized bed reactors 1 to 4 are included with respect to the transmission of the reducing gas not only sequentially, but also with regard to the transmission of a small portion of the reducing gas, while the fluidized bed reactors 1 to 4, as regards the discharge and further passage of the reducing gas, included in this example implementation, exclusively, sequentially.

 According to the installation shown in FIG. 2, the heating of the reducing gas is carried out in two stages, namely, in the first stage, by heat exchange in the gas heater 19, and in the second stage, by partial combustion in the device for partial combustion using oxygen supplied to the reducing gas through the pipe 32.

It is preferable to bring the gas to be heated, first in the gas heater 19, operating as an indirect heat exchanger, to a temperature in the range from 200 to 600 ^o C. Heat can be supplied by burning any fuel, preferably natural gas, removed from the recovery process.

Further heating of the reducing gas to temperatures, preferably 700 - 900 ^o C can be carried out in the following options:
a) by separating part of the reducing gas and stoichiometric combustion with pure oxygen (if necessary, you can also take a mixture with air). This partial stream is mixed with the remaining, cooler reducing gas in such a way that the desired final temperature of the total reducing gas stream is set;
b) by introducing all of the reducing gas into the combustion chamber and partial combustion (i.e. below stoichiometric). The desired final temperature is established by back-mixing the burnt gases with unburnt ones.

 Using this type of heating, the problem of eliminating metal dusting is solved, and the process is economical due to insignificant pressure losses in the partial combustion furnace compared to conventional indirect heating furnaces.

Partial combustion also changes the composition of the reducing gas, usually the proportion of H ₂ O increases in favor of the H ₂ content by 1-5% vol. This also applies to the CO ₂ content in favor of the CO content.

Therefore, in order to establish a certain chemical composition of the reducing gas after heating, an appropriate method is necessary before heating. This is possible with the help of the changing technology of CO ₂ purification, reforming, etc. So, for example, one can easily compensate for the production of CO ₂ by partial combustion, for example, by installing at the outlet of the adsorption device 16 a variable pressure of a lower CO ₂ content. The loss of CO due to partial combustion can be compensated by changing the reforming technology (for example, a lower vapor / carbon ratio) or, for example, by increasing the bypass flow to the CO conversion. The same applies to the regulation of H ₂ and H ₂ O.

 Since in the adsorption device 16 of variable pressure, a reducing gas is obtained with 0% vol. water, the water content in the reduced gas to the reduction reactors — that is, after heating in the partial combustion furnace — can be kept very low (in the range of 1 to 2% vol.).

 The invention is not limited to the exemplary embodiments shown in the drawing, but can be modified in various directions. For example, it is possible to select the number of reactors according to need. Instead of a variable pressure adsorption device 16, an adsorption process with a change in temperature can also be used. The former use high pressure in the system in the corresponding process of direct reduction, that is, adsorption and regeneration of the adsorbent is carried out by creating different pressures in the tank, and external energy is not required for supply, but pressure directly in the system can be used. In the second variant, adsorption at a variable temperature (TSA - Temperature Swing Adsorption), the adsorption and regeneration process is controlled by the temperature profile at an almost constant pressure. The adsorption capacity of the active medium depends, along with pressure, also on temperature. In the field of application under consideration, this method acts as the second option, since variable pressure adsorption for the applied compositions of the reformed gas and blast furnace gas, as well as for the pressure present in the system, is preferred.

Example A
In the installation of FIG. 1 with an hourly output of 75 t / h of hot briquetted iron, 104 t / h of ore fines took part in the reaction.

In steam reformer 10, 108,000 Nm ³ / hr of reformed gas are obtained by reacting 18,100 Nm ³ / hr of natural gas with 60,300 Nm ³ / hr of steam. The amount of heat required for heating, equal to 94 MW, was covered by natural gas (61 MW), preheated air (23 MW) and exhaust gas (10 MW).

70% of the reformed gas was mixed with recirculated blast furnace gas and, after cooling to 40 ^° C., was supplied to a variable pressure adsorption device 16 at a pressure of 14.25 bar. The purified gas at a temperature of 45 ^o C and a pressure of 13.45 bar was mixed with flowing gas flows in the amount of 179900 Nm ³ / h and brought to the reducing gas heater 19.

The separated off-gas - 22900 Nm ³ / hr is at a pressure of 0.3 bar, at a temperature of 35 ^o C and an energy content of 60 MW.

To heat the reducing gas to 835 ^° C, 65 MW of 50 MW of waste gas, 14.7 MW of preheated air and 0.3 MW of blast furnace gas are needed.

 Hot briquetted iron has a metallization ratio of 92%.

 The gas composition is as follows (see table. 1).

Compared with the prior art, according to the invention, a reducing gas is obtained with a significantly lower content of N ₂ or CH ₄ (for example, according to EP-A - 0571358: 14.94% vol. N ₂ , 16.29% vol. CH ₄ ) and therefore improved recovery ability.

The ore fines used have 96.91 wt.% Fe ₂ O ₃ and 2.29 wt.% Gangue, the rest is firing losses.

Example B
In the installation of FIG. 1 with an hourly output of 75 t / h of hot briquetted iron, 104 t / h of ore fines took part in the reaction.

The steam reformer 10 received 100,100 Nm ³ / hr of reformed gas by reacting 17,200 Nm ³ / hr of natural gas with 55,700 Nm ³ / hr of steam. The amount of heat required for heating, amounting to 86 MW, was covered with natural gas (25 MW), pre-heated air (21 MW) and exhaust gas (40 MW).

90% of the reformed gas was mixed with 60% of the recirculated top gas and, after cooling to 40 ^° C., was supplied to a variable pressure adsorption device 16 at a pressure of 14.25 bar. The purified gas at a temperature of 45 ^o C and a pressure of 13.45 bar was mixed with the flowing gas flows - in the amount of 184000 Nm ³ / h and brought to the reducing gas heater 19.

The separated off-gas - 29900 Nm ³ / hr is at a pressure of 0.3 bar, at a temperature of 35 ^o C and with an energy reserve of 87 MW.

To heat the reducing gas to 835 ^o C, it is necessary 68 MW obtained from 47 MW of exhaust gas, 15 MW of preheated air and 6 MW of blast furnace gas.

 Hot briquetted iron has a metallization ratio of 92%.

 The gas composition is as follows (see table. 2).

A significant difference between examples A and B is the different contents of CH ₄ in the reducing gas. Although CH ₄ acts in relation to the actual recovery as an inert component, but, nevertheless, affects the quality of the product. In example A, the content of CH ₄ in the reducing gas at approximately 12.8% vol., In example B at 18.8% vol., Which later leads to a higher carbon content in the briquetted product. This higher carbon content may (but not necessarily) be an advantage in certain product variations. For example, a higher carbon content during the further production of steel in an electric furnace can lead to energy savings during melting.

The ore fines used have 96.91 wt.% Fe ₂ O ₃ and 2.29 wt.% Gangue, the rest are firing losses.

Example C
In the installation of FIG. 1 to obtain 75 t / h of hot briquetted iron, the following form of obtaining reducing gas was chosen:
- obtaining 130,000 Nm ³ / h of reformed gas with the same composition as in example A;
- 100% of the reformed gas after cooling was supplied to the variable pressure adsorption device 16;
- thus purified gas was mixed with recirculated top gas;
- gas flows in the amount amounted to 181000 Nm ³ / h - brought to the heater 19 of the reducing gas.

 Hot briquetted iron had a metallization ratio of 92%.

 The gas composition is as follows (see table. 3).

 Iron ore had the same composition as in example A.

Advantages with this gas distribution:
a decrease in the power of an adsorption device of variable pressure (comparable with examples A and B from 30 to 40%);
the exhaust gas does not contain H ₂ S (in examples A and B it was introduced with iron ore into the top gas circuit and partially shut off in a variable pressure adsorption device) - due to this, subsequent thermal use of the exhaust gas does not produce SO ₂ harmful to the environment environment, and you can abandon the desulfurization device.

Claims (12)

1. A method for the direct reduction of a fine-grained particle containing iron oxide in the form of particles in a fluidized bed, wherein the reformed gas, purified at least partially from CO ₂ , is supplied as a reducing gas to the recovery zone of the fluidized bed and removed from it as blast furnace gas, and moreover, blast furnace gas is used for direct reduction at least partially together with the reformed gas, characterized in that from 50 to 100% of the reformed gas and 0 to 100% of the blast furnace gas In addition to CO ₂ , at least partially CH ₄ and N _{2 are} obtained by adsorption, preferably by pressure adsorption, the reducing gas is heated and the exhaust gas separated from the reformed gas or blast furnace gas by adsorption is used as a combustible gas.  2. The method according to p. 1, characterized in that the exhaust gas separated from the reformed gas or blast furnace gas by adsorption by alternating pressure is used to heat the reducing gas and / or as combustible gas for the reforming process upon receipt of the reformed gas. 3. The method according to claim 1 or 2, characterized in that the reformed gas is cooled before removal of CO ₂ , if necessary by mixing with blast furnace gas, preferably to a temperature of 20-100 ^o C, in particular between 30-50 ^o C.  4. The method according to one or more of claims 1 to 3, characterized in that the direct reduction of the particulate material containing iron oxide is carried out in several successively connected reduction zones in the fluidized bed, and the particulate iron-containing material is directed from one fluidized bed zone to another zone with a fluidized bed under the action of gravity from top to bottom, and the reducing gas is passed from one zone with a fluidized bed to another zone with a fluidized bed countercurrent, m reducing gas used in direct reduction, as blast furnace gas, is withdrawn from the uppermost recovery zone with a fluidized bed, mixed with reformed gas and used as reducing gas.  5. The method according to one or more of claims 1 to 4, characterized in that the heating of the reducing gas is carried out in two stages, namely: in the first stage (19) by heat exchange and in the second stage (31) by partial combustion with oxygen, supplied to at least a portion of the reducing gas (figure 2). 6. Installation for implementing the method according to one or more of claims 1 to 5, containing at least one reactor (1 - 4) with a fluidized bed for receiving iron-containing material, a pipeline (18) for supplying reducing gas to this reactor (4) a fluidized bed and a pipe (8) for diverting from the reactor (1) with a fluidized bed of top gas generated during reduction, a reformer (10), a reformed gas pipeline (13) that goes from the reformer (10), which is connected to the pipeline (8) for top gas, moreover reducing gas obtained from reformed gas and blast furnace gas, through a pipe (18) for supplying reducing gas enters the reactor (4) with a fluidized bed and a device (16) for cleaning from CO ₂ , characterized in that the device (16) for cleaning CO _{2 is} made in the form of an adsorption device, preferably in the form of an adsorption device with a variable pressure, a pipeline supplying gas purified from CO ₂ from an adsorption device (16) to a heating device (19) and a pipeline (16 ''), exhaust gas , released in the adsorption device, lead to a heating device.  7. Installation according to claim 6, characterized in that the adsorption device (16) is shunted by a branch pipe (22) for blast furnace gas, and, if necessary, a branch pipe (21) for reformed gas, leaving the pipe (13) with reformed gas.  8. Installation according to claim 6 or 7, characterized in that the pipeline (16 '') for exhaust gas removal is connected to the reformer heating device (10).  9. Installation according to one or more of claims 6 to 8, characterized in that the pipeline (16``) for exhaust gas removal is connected to a heating device (19) for reducing gas.  10. Installation according to one or more of claims 6 to 9, characterized in that there is a gas cooler in the pipeline for supplying gas to the adsorption device (17).  11. Installation according to one or more of claims 6 to 10, characterized in that several fluidized bed reactors (1 to 4) are connected in series with each other, and material containing iron oxide is supplied from one fluidized bed reactor (1) to another reactor (2, 3, 4) with a fluidized bed through transport pipelines (6) in one direction, and the reducing gas is passed from one reactor (4) with a fluidized bed to another reactor (3, 2, 1) with a fluidized bed through connecting piping (20) in the opposite m direction and wherein within each of the reactor (1 - 4) from the fluidized bed are cyclones for precipitation of small particles entrained in a reducing gas.  12. Installation according to one or more of claims 6 to 11, characterized in that there is a heat exchanger (19) and a device (31) connected in series with it for partially burning the reducing gas with oxygen supply (32) as a heating device for reducing gas.

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