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    • 专利摘要:
    Shown is a method for removing CO 2 from exhaust gases (4) of pig iron production plants or synthesis gas plants, wherein the CO 2 purified waste gases are then used in a direct reduction plant (33). It is characterized in that the CO 2 is removed by chemical absorption (1) from the waste gas (4) withdrawn from the process of pig iron production or syngas production before its use in a direct reduction plant (33), the heat being used for regeneration of the absorbent is provided, at least in part, either by low pressure steam used from a steam turbine of a steam power plant and / or a steam turbine to utilize the waste heat from the pig iron production, and / or by low pressure steam from a waste heat boiler (16) Steam power plant and / or from a waste heat boiler (6, 7, 58, 61, 92) for using the waste heat from the pig iron production and / or from a waste heat boiler (59) for using the heat from the direct reduction plant (33), - and / or an air separation plant, - and / or from process gases (22, 26, 29, 69) of plants for the production of pig iron, synthesis gas (98) and / or from direct reduction plants (11, 46, 52). As a result, the CO 2 can be separated from exhaust gases of pig iron production to a greater extent than with pressure swing adsorption of other gases and it can also be used for a lower energy source but in addition.
    公开号:AT510618A1
    申请号:T1819/2010
    申请日:2010-11-04
    公开日:2012-05-15
    发明作者:Robert Dipl Ing Millner
    申请人:Siemens Vai Metals Tech Gmbh；
    IPC主号:
    专利说明:

    200817716 1
    ·· * * · ··· ·· «
    description
    Method for removing CO2 from exhaust gases
    The invention relates to a method for the removal of CO 2 from exhaust gases from plants for pig iron production or synthesis gas plants, the CO2 purified from exhaust gases are then used in a direct reduction plant, ie the combination of a plant for pig iron production or a synthesis gas plant with on the other hand a direct reduction plant. This direct reduction plant is an independent plant and is not identical with the reduction reactor (s) or reduction shaft (s) that may be present in the plant for the production of pig iron.
    For the production of pig iron, which should also include the production of pig iron-like products, there are essentially two known common processes: the blast furnace process and the smelting reduction.
    The blast furnace process first produces pig iron from iron ore using coke. In addition, scrap can also be used. Thereafter, steel is produced by further processes from pig iron. The iron ore is used as lump, pellets or sinter together with the reducing agents (usually coke, or else coal, for example in the form of a
    Fine coal indisposition plant) and other constituents (limestone, slag formers, etc.) are mixed to form the so-called Möller and then charged into the blast furnace. The blast furnace is a metallurgical reactor in which the Möllersäule reacts in countercurrent with hot air, the so-called hot blast. By burning the carbon from the coke, the heat and carbon monoxide or hydrogen necessary for the reaction are produced, which constitutes a substantial part of the reducing gas and flows through the Möller column and reduces the iron ore. The result is pig iron and slag, which are tapped periodically. 5
    In the so-called oxygen blast furnace, which is also referred to as a blast furnace with top or top gas recirculation, in the gasification of coke or coal oxygen-containing gas with more than 80% oxygen content (O2) is injected into the blast furnace 10. For the gas leaving the blast furnace, the so-called top or top gas, a gas cleaning must be provided (for example dust collectors and / or cyclones in combination with 15 wet scrubbers, bag filter units or hot gas filters). Furthermore, the oxygen blast furnace usually a compressor, preferably provided with aftercooler, provided for the top gas returned to the blast furnace and a device for C02 ~ removal, according to the prior art usually by means of pressure swing adsorption 20.
    Further options for the design of a blast furnace process are a heater for the reducing gas and / or a combustion chamber for the partial combustion with oxygen.
    The disadvantages of the blast furnace are the demands on the feedstock and the high emission of carbon dioxide. The iron carrier used and the coke must be lumpy and hard, so that sufficient cavities remain in the Möllersäule, which ensure the flow through the blown wind. C02 emissions represent a heavy environmental impact. Therefore, there are efforts to replace the blast furnace route. These include 35 natural gas sponge ironmaking (MIDREX, HYL, FINMET) and smelting reduction processes (COREX® and FINEX® processes). 3 3 * 4 ♦ 200817716
    In the smelting reduction, a melter gasifier is used in which hot liquid metal is produced, and at least one reduction reactor in which the carrier of the iron ore (lump, fine ore, pellets, sinter) is reduced with reducing gas, the reducing gas in the melter gasifier by gasification of Coal (and possibly a small proportion of coke) is produced with oxygen (90% or more).
    Also in the smelting reduction process are usually - gas purification plants (on the one hand for the top gas from the reduction reactor, on the other hand for the reducing gas from the melter gasifier), - a compressor, preferably with aftercooler, for the recirculated into the reduction reactor reducing gas, - a device for C02 ~ removal , According to the prior art usually by means of pressure swing adsorption - and optionally provided a heater for the reducing gas and / or a combustion chamber for partial combustion with oxygen.
    The COREX® process is a two-stage process
    Smelting reduction. The smelting reduction combines the process of direct reduction (prereduction of iron into sponge iron) with a melting process (main reduction).
    The well-known FINEX® process essentially corresponds to the COREX® process, but iron ore is introduced as fine ore.
    The invention can be applied not only to pig iron production but also to synthesis gas plants. Synthesis gases are all hydrogen-containing and usually also CO-containing gas mixtures which are to be used in a synthesis reaction. Synthesis gases can be made from solid. 4 200817716 liquid or gaseous substances are produced. In particular, this includes coal gasification (coal is converted with water vapor and / or oxygen to hydrogen and CO) and the production of synthesis gas from natural gas (conversion of methane with water vapor and / or oxygen to hydrogen and CO). Synthesis gas plants also produce unwanted CO2, which has to be separated.
    In any case, part of the invention is also a direct reduction plant. In a direct reduction plant lumpy iron ore carriers (lump ore, fine ore or pellets (fine-grained iron ore is rolled with water, binders and aggregates to green pellets and hardened in a final firing)) in the solid state at 750-1000 ° C reduced by reducing gas or coal. The result is directly reduced iron (English: direct reduced iron, short DRI), which is also referred to as sponge iron. The direct reduction plant contains as its core either a reduction shaft in the sense of a fixed bed reactor or fluidized bed reactors into which or into which the lumpy iron ore and the reducing gas (or the coal) are introduced. In the following, the term "reduction well" will be used. used for both fixed and fluidized bed reactors.
    However, a direct reduction plant can also be used to connect the directly reduced iron to larger units, ie hot briquetting, so that from the discharged from the reduction shaft DRI by means of a Heißbrikettieranlage so-called hot briquetted iron (short: HBI) arises. Also so-called low-reduced iron (English: low reduced iron, short LRI) can be deducted from the reduction shaft with appropriate process guidance.
    In order to reduce CO 2 emissions into the atmosphere during the production of pig iron or synthesis gas, the 5 200817716 C02 must be separated from the waste gases of pig iron production or synthesis gas production and stored in bound form (CO2 Capture and Sequestration (CCS)). ).
    For the deposition of CO 2 mainly the pressure swing adsorption (English: PSA - Pressure Swing Adsorption), in particular also the vacuum pressure swing adsorption (English: VPSA - Vacuum Pressure Swing Adsorption) is used. Pressure swing adsorption is a physical process for the selective decomposition of gas mixtures under pressure. Specific porous materials (eg zeolites, activated carbon, activated silica (SiO 2), activated alumina (Al 2 O 3) or the combined use of these materials) are used as a molecular sieve to adsorb molecules according to their adsorption forces and / or their kinetic diameters. The PSA exploits the fact that gases adsorb to surfaces to different extents. The gas mixture is introduced into a column under a well-defined adsorption pressure, to the gas mixture of 1.5-2 barg after exiting the plant for pig iron production to be compressed to 3-7 barg, which is done by large turbocompressors with high electrical power consumption , (Synthesis gas plants, on the other hand, usually supply the synthesis gas at 15-30 barg, which means that compaction is no longer required.) For this reason, the CU2 removal is carried out using absorption processes (often a physical absorption process such as Rectisol® is used).
    Now adsorb the unwanted components (here CO2 and H20) and the recyclable material (here CO, H2, CH4) flows mostly unhindered through the column. Once the adsorbent is fully loaded, the pressure is reduced and the column rinsed. To operate a (V) PSA plant, electrical power is needed for the prior compression of the CO 2 rich recycle gas. 6 200817716
    The product gas stream after the pressure swing adsorption, which contains the recyclable materials, still contains about 2-6 vol% CO2 at 2.8-6.8 barg for exhaust gases from pig iron production.
    Depending on the reduction unit, the pressure energy of the product gas must be reduced again via control valves and is therefore lost. By returning the top gas from the direct reduction plant, the nitrogen content in the reducing gas increases, which entails a higher energy consumption for the reduction gas heater and, on the other hand, also increases the productivity of the reducing gas
    Reduction shaft or the fluidized bed reactor reduced. However, the residual gas stream from the (V) PSA plant still contains relatively high reducing gas constituents (such as CO, H2), which are lost for direct reduction and thus reduce the capacity of the direct reduction plant.
    The residual gas stream after pressure swing adsorption, which contains the undesirable components, is typically composed of exhaust gases from pig iron production as follows:
    Compound vol% at VPSA vol% h2 2.2 5.5 n2 1.5 2.4 CO 10.9 16.8 C02 82.1 72.2 ch4 0.7 0.9 h2o 2.6 2.2
    The residual gas thus still contains a high proportion of combustible materials with a calorific value in a range typically 1800-4000 kJ / m 3 N and has a pressure of slightly above ambient pressure.
    The residual gas can not simply be utilized thermally because, due to the low and / or fluctuating temperature, it is possible, due to the low and / or fluctuating temperature. · · Φ φ ♦ φ · «
    Calorific value - would have to be enriched with other fuels.
    If the CO2 from the residual gas is to be bound, the residual gas must be compressed so that the C02 is in liquid form, and then the liquid CO 2 must be placed in a reservoir, to which the pressure must usually be increased so far that the CO 2 is in the liquid-solid or supercritical state, where CO2 has a density of about 1000 kg / m3.
    The supercritical state is a state above the critical point in the phase diagram (see FIG. 1) which is characterized by the equalization of the densities of the liquid and gas phases. The differences between the two states of aggregation cease to exist at this point.
    Such a high compression requires the use of a high power multi-stage compressor to bring the typical line-level densities in the range of greater than 0 ° C and greater than 70 bar (7,000,000 Pa), more preferably 80-150 bar at ambient temperatures, is located.
    However, the residual gas from a (V) ΡΞΑ is not suitable for being bound because it has a relatively high proportion of CO, H2, N2, CH4, etc. in addition to CO2. On the one hand, the CO content poses a safety risk, as this can lead to a risk of injury to persons (CO poisoning) and, under certain circumstances, to inflammation or explosion. Furthermore, the "impurities" CO, H2, ... of the CO2 lost for the reduction work and influence the physical properties of the compressed gas, for which fluctuate due to the fluctuating levels of CO, H2, etc, the measurability, the compression, the solubility and the transport properties also. 8 200817716
    Contaminants must also reduce the distances between stations where the transported gas mixture or liquid must be recompressed, increasing investment and operating costs due to additional compressors or pumps and their energy requirements. Or, the inlet pressure in the line must be increased to reduce the number or power of the additional pumps and compressors along the line.
    Investigations into the influence of contaminants on the transport of liquefied gases have been carried out by Newcastle University and published at http://www.ge0s.ed.ac.uk/cc5/UKCCSC/Newcastle 2 07, ppt, and are shown in FIG ,
    It is therefore an object of the invention to separate the CO 2 from exhaust gases of pig iron production or synthesis gas production to a greater extent than in (V) PSA from other gases in direct reduction plants, which are connected to plants for pig iron production or synthesis gas plants, but in addition one lower energy source than (V) PSA.
    The object is achieved by a method according to claim 1, characterized in that the CO 2 is removed by means of chemical absorption from the exhaust gas, which was withdrawn from the process of pig iron production or syngas production, before its use in a direct reduction plant, wherein the heat for the regeneration of the absorbent at least partially - provided either by low pressure steam, which is used from a steam turbine of a steam power plant and / or a steam turbine to use the waste heat from the pig iron production, - and / or by low pressure steam from a waste heat boiler of a steam power plant and / or from a waste heat boiler for use the waste heat from pig iron production and / or from a waste heat boiler for utilizing waste heat from the direct reduction plant, and / or from an air separation plant, and / or from process gases from plants for the production of pig iron, from synthesis gas plants and / or from direct reduction plant is related.
    Under "low pressure steam" Steam is understood as being saturated and having a pressure between 1 and 15 barg.
    Under the term "steam power plant " fall on the one hand conventional steam power plants, where thermal energy is generated by combustion of fuels, with which steam is produced, which is utilized in a steam turbine, that is ultimately converted into electrical energy.
    On the other hand, this also includes a combined cycle power plant, more specifically a combined cycle power plant (CCPP), in which the principles of a gas turbine power plant and a steam power plant are combined. A gas turbine serves as a heat source for a downstream waste heat boiler, which in turn acts as a steam generator for the steam turbine.
    Under "Air Harvesting System" This is a system in which air is first compressed, liquefied and then broken down into individual components (oxygen, nitrogen, noble gases).
    By using a chemical absorption process, the proportions of the recovered gases for direct reduction CO, H2, CH4 compared to a (V) PSA can be increased in the purified exhaust gas of the pig iron production or synthesis gas production and the CO 2 fraction in the product gas substantially (up to a few ppmv ) are reduced. Thus, the plant performance of the direct reduction plant, 200817716 10
    ···· * ·
    So the iron and / or briquette production (DRI, HBI, LRI) are increased.
    The exhaust gas withdrawn from the process of pig iron production or syngas production is often called " export gas " designated. In particular, it serves as a name for that part of the top gas that is withdrawn from the process of pig iron production. The export gas must normally be compressed, such as by means of one or two-stage centrifugal compressors, and then cooled, e.g. can be used or stored as fuel gas. The direct forwarding of the export gas from pig iron production or synthesis gas production to chemical absorption eliminates the hitherto necessary compressors and coolers for the export gases.
    The use of low-pressure steam from an existing steam process is less expensive than the production of steam with its own aggregate only for desorption. In addition, the use of a low-value energy source such as steam from an economic and environmental point of view is preferable to a high-quality energy source such as electricity. The removal of steam from a running steam power plant is also more flexible than from a specially operated for CCh steam generator, the fuel for steam generation is better utilized in a continuous steam process.
    Likewise, the use of already existing heat to regenerate the absorbent from other equipment is less expensive than the provision of heat from specially purchased equipment. Thus, for example, the heat from air separation plants or from process gases which are present anyway in the process according to the invention can be used, for example heat from the process gases of plants.
    Pig iron production, synthesis gas plants and / or direct reduction plants.
    The residual gas stream after the chemical absorption mainly contains CO2 and after removal of H2S only traces of H2S and can therefore be discharged directly into the atmosphere and / or just fed to a C02 compression followed by CO 2 storage (English: sequestration, eg EOR - enhanced oil recovery) and / or as a substitute for inert gases such as N2, for example in iron production: the residual gas stream consists mainly of CO 2 and can therefore be used for charging equipment, barrier seals and selected rinsing and Cooling gas consumers are used.
    Due to the low level of impurities, the energy required to compress the residual gas stream from chemical absorption to liquid-solid or supercritical (> 73.3 bar) is about 20-30% lower than residual gas from a (V) PSA , Consequently, the distances between the stations increase in the gas lines, where the gas must be re-compressed. Both the acquisition costs and the operating costs for C02 storage are thereby reduced.
    Compared to pressure-swing adsorption, chemical absorption works with lower pressures on the gas to be cleaned and a lower pressure drop on removal of CO 2, which also saves energy. In contrast to a VESA, no vacuum compressors are needed, which also consume a lot of energy and cause high maintenance costs. The low energy consumption is an advantage especially for those countries where energy is scarce and / or expensive.
    The investment costs for a chemical
    Absorption methods are similar to those for a 200817716 12
    Mt • ts «· * VPSA system. But the absorption process needs large amounts of low-pressure steam with a pressure of more than 2 barg or higher, e.g. 10 barg. This steam would be expensive if it had to be specially made and could not be taken from an existing steam source.
    There are several chemical absorption methods suitable for this invention:
    A first absorption process is characterized by the use of potassium carbonate as the absorbent. Hot Potassium Carbonate (HPC) or " Hot Pot " is used. Depending on the supplier of this process, various substances are added to the potassium carbonate: activators which are intended to increase CO 2 deposition and inhibitors which are said to reduce corrosion. A widely used method of this type is known as the Benfield method and is offered by ÜOP. The Benfield process requires about 0.75 kg of steam per Nm3 of gas to be cleaned.
    A second absorption process is known as amine scrubbing with several sub-processes. In a first step, slightly alkaline aqueous solutions of amines (mostly ethanolamine derivatives) are used which reversibly chemically absorb the acidic gases, for example the CO 2. In a second process step, the acidic gas is thermally separated (by heating) from the amine and the recovered amine is used again for washing.
    Known methods for this are the Amine Guard FS method from UOP, which reduces the CO 2 content to 50 ppmv and the H2S content to 1 ppmv. The steam requirement of this process is about 1.05 kg of steam per Nm3 of gas to be purified. 13 13 200817716 t »*« «« «ι ·« «» ·· < - > · «*« · * «« «« * * * «« «* * * ·
    Amines, such as diethanolamine (DEA), are also used as activators for absorption processes using potassium carbonate, such as the Benfield process. For amine scrubbing primary amines can be used, such as methylamine, monoethanolamine (ΜΕΔ) and / or diglycolamine (DGA). For amine scrubbing, secondary or secondary amines may be used in addition to or as an alternative to primary amines, such as diethanolamine (DEA) and / or diisopropanolamine (DIPA).
    In addition or as an alternative to primary and / or secondary amines, it is also possible to use tertiary amines, for example triethanolamine (TEA) and / or methyldiethanolamine (MDEA). An existing process for this purpose is the aMDEA process from BASF (offered by Linde and Lurgi), which uses activated methyldiethanolamine (MDEA). The steam requirement of this process is about 0.85 kg of steam per Mm3 of gas to be purified.
    Other methods are based on amino acid salts.
    Advantageously, with the method according to the invention, top gas from a blast furnace, in particular from an oxygen blast furnace with top gas recirculation, which is operated predominantly with oxygen instead of hot blast, can be purified of CO.sub.2 and then fed to the direct reduction plant as reducing gas. Equally advantageously, the exhaust gas from a smelting reduction plant and / or the synthesis gas of a synthesis gas plant can be cleaned and then the
    Direct reduction system to be fed as a reducing gas.
    The exhaust gas withdrawn from the process of pig iron production or syngas production is therefore called "export gas". referred to, because it - if necessary after cleaning and / or cooling - from the pig iron or 14 14 • 4 «·» I r * 200817716
    It may consist of the following process gases: - Topgas from a blast furnace, - Excess gas from a smelting reduction plant, - Topgas from a smelting reduction plant, such as from a reduction shaft, a reduction reactor or from a fixed bed reactor for preheating and / or reduction of iron oxides and / or iron briquettes - generator gas from a smelting reduction plant, ie exhaust gas from the melter gasifier. As a gas generator, a very CO-containing gas is referred to, which is produced by gasification of coke - residual gas from a plant integrated in the plant for pig iron production (blast furnace or smelting reduction) for CO 2 removal, such as a (vacuum) pressure swing adsorption.
    Top gas or blast furnace gas is the gas emerging from the blast furnace or a reduction shaft at the top.
    Waste gas from the melter gasifier, which is currently not required in the smelting reduction process and therefore has to be removed from the gas system of the smelting reduction process, is referred to as excess gas. It may again be top or generator gas.
    To easily obtain low pressure steam, this is best taken at the end of the expansion of the steam turbine or the waste heat boiler of the steam turbine.
    However, the heat required for the regeneration of the absorbent can also be taken from process gases: from the process gases from plants for the production of pig iron can - excess gas from a smelting reduction plant, - top gas from a smelting reduction plant or from a blast furnace,
    200817716 15 «* * * ♦ * " «* 9 * ♦ ~ Generator gas from a smelting reduction plant and / or residual gas from a C02 removal plant integrated into the pig iron production plant. Thus, the heat of that exhaust which is to be purified of CO2 can also be used for the regeneration of the chemical absorption absorbent.
    Consequently, heat can also be withdrawn from the synthesis gas of the synthesis gas plant (for example a gasification plant) for the purpose of regenerating the absorbent of the chemical absorption.
    Heat from the process gas of direct reduction plants, such as the top gas or the cooling gas, can be used for the regeneration of the absorbent, as well as the waste heat of the exhaust gas from the reduction gas furnace (heating unit) of the direct reduction plant.
    The energy required for the regeneration of the absorbent can also be made available by passing hot air from the air separation plant into a heat exchanger for heating and regeneration of the absorbent. For example, hot air may be used from the main air compressor and / or the booster air compressor.
    The heat from the air separation plant may also be provided to regenerate the absorbent by means of a heat transfer medium (e.g., water vapor) heated by hot air from the air separation plant (from the main air compressor and / or the booster air compressor).
    The CO2-rich gas obtained from the chemical absorption can, if necessary after compression to 5-11 barg, be used as substitute gas for nitrogen in the production of pig iron, in synthesis gas production, in direct reduction and / or in 2008. * * * I ff II * «4 4 t» i 4 * 44 «« 4 I * «I« 44 4 * 4 4 «* 4 44 4 used for the treatment and storage of CO2. The CO2 rich gas can be used in pig iron production, direct reduction and coal gasification to replace nitrogen for Charger, barrier seals and selected Spül- and Kühlgasverbraucher, such as for the seal of the reduction shaft of the direct reduction plant or for the charging facilities of the fluidized bed reactor of the direct reduction plant or for the dynamic Gas barrier devices of the charging and removal device of the direct reduction plant. The use of C02 instead of nitrogen also reduces energy consumption in the process gas streams because of the lower nitrogen content.
    The heat generated in the compression of the C02 gas can also be used for the regeneration of the absorbent.
    In a device according to the invention comprising a direct reduction plant and a CO 2 removal plant by means of chemical absorption, it is provided that at least one line from the CC > 2 deposition plant leads to the reduction well of the direct reduction plant to recover the CO 2 purified Exhaust gases then use in the direct reduction plant, and in the plant for CO 2 deposition at least one line opens for exhaust gas, which from the process of
    Cast iron production or synthesis gas production was withdrawn, and the part of the plant for the regeneration of the absorbent - either connected to a steam turbine of a steam power plant or a steam turbine to use the waste heat from the pig iron production, that low-pressure steam from the steam turbine at least partially passed into the plant part for the regeneration of the absorbent can be - and / or connected to the waste heat boiler of a steam power plant 17 17 * · Μ * · 200817716 and / or the waste heat boiler for using the waste heat from the pig iron production and / or the waste heat boiler for the use of waste heat from the direct reduction plant, that the Waste heat can be used at least partially to generate low-pressure steam for the regeneration of the absorbent, - and / or is connected to a Luftzerlegungsanlage that the heat from the air separation plant will be used at least partially for the regeneration of the absorbent n can, and / or is connected to plants for pig iron production, synthesis gas plants and / or direct reduction plants, that heat from the process gases of these plants can be used at least partially for the regeneration of the absorbent.
    In particular, a line can be provided for the blast furnace process, with which top gas from a blast furnace, in particular from an oxygen blast furnace with Topgasrückführung, can be fed into the plant for the removal of COj by means of absorption.
    In a smelting reduction process, at least one line would then be provided, with which exhaust gas can be passed from a smelting reduction plant into the plant for the removal of CO 2 by means of absorption. In a synthesis gas plant, at least one conduit would be provided, with which synthesis gas can be fed into the plant for the removal of CO2 by absorption.
    For introducing low-pressure steam into the system for the removal of CO 2 can be provided that it is connected to the low pressure part of the steam turbine and / or the waste heat boiler. 18 200817716 • · · · »«
    There are also various physical absorption methods that could be used in this invention instead of the chemical absorption process, which of course excludes pressure swing absorption. But such physical absorption methods are mainly useful if the export gas from a synthesis gas plant, because here the properties of the export gas in terms of pressure and temperature are better matched to the physical absorption process, which require a higher pressure in the gas to be cleaned. It would not make economic sense to compress export gas from the pig iron production only with energy expenditure in order to deposit the CO 2 in a physical absorption process.
    Chemical absorption processes are characterized by the fact that the gas to be separated with the absorption agent partially or completely forms a solid or loose chemical bond. In a physical absorption process, the gas to be separated is dissolved in the absorbent without changing its material properties, the van der Waals forces act. In addition, there are still methods in which both chemical and physical bonding forces come into play and which are referred to as hybrid washes.
    Some of the most important representatives of suitable physical absorption processes are the so-called Purisol® process, the Rectisol® process and the Selexol process.
    The Purisol® process utilizes N-methyl-2-pyrrolidone (NMP) as the absorbent, regenerating the absorbent via steam through indirect heat exchangers, with a steam demand of approximately 1562 kg / MM scf = approximately 0.058 kg / Nm3 , It can handle all kinds of 200817716 19 • * * * *
    Heat exchange media can be used: air, nitrogen, steam, thermal oil, etc ..
    In the Rectisol® process, cooled methanol (CH3OH) is used as the absorbent. The regeneration of the absorbent is carried out by means of steam via indirect heat exchangers, wherein the absorbent is heated to only about 65 ° C. The steam requirement is about 1275 kg / MM scf = about 0.047 kg / Nm3 gas to be cleaned. All types of heat exchange media can be used: air, nitrogen, steam, thermal oil, etc.
    In the Selexol process, the absorbent used is a mixture of dimethyl ethers of polyethylene glycol. Regeneration is by steam, requiring direct contact of the absorbent with steam or an inert gas (e.g., nitrogen).
    The invention is explained in more detail below with reference to the exemplary and schematic figures.
    Fig. 1 shows a phase diagram of CO2.
    Fig. 2 shows the relationship between impurities of gases and the compaction stations necessary for the transport of liquefied gases.
    3 shows the connection according to the invention between a smelting reduction plant (COREX® plant) and a direct reduction plant.
    4 shows the connection according to the invention between a smelting reduction plant (FINEX® plant) and a direct reduction plant.
    Fig. 5 shows the connection according to the invention between an oxygen blast furnace and a direct reduction plant.
    Fig. 6 shows the connection according to the invention between a coal gasification plant and a direct reduction plant. 20 20 • · 200817716
    FIG. 1 shows a phase diagram of CO 2. On the horizontal axis the temperature is plotted in K, on the vertical axis the pressure in bar (1 bar = 105 Pascal). The individual states of matter (solid or solid, liquid or liquid and gas or gaseous) are separated by lines.
    The triple point is the point where solid, liquid and gaseous phases meet.
    The supercritical state (supercritical fluid) is a state above the critical point in the phase diagram, which is characterized by the equalization of the densities of the liquid and gas phases. The differences between the two states of aggregation cease to exist at this point.
    In Fig. 2, the relationship between impurities of gases and the compaction stations necessary for the transport of liquefied gases is shown.
    On the horizontal axis the impurities in% of the gas volume are plotted, on the vertical axis the distance between the compressor stations in km. For each contamination, a separate curve is drawn. At 10% contamination (right margin of illustration), the least effect on the distance of the compressor stations in H2S, followed by S02, CH4, Ar, 02, N2 and CO is the same, then N02, the greatest influence is H2, where the curve almost goes to zero.
    3 shows the connection according to the invention between a plant for smelting reduction (namely a COREX® plant 32), a direct reduction plant 33 with a plant 1 for the chemical absorption of CO 2 and a steam generating plant 34.
    The chemical absorption system 1 of C02 consists essentially of an absorber 8, a stripper 9 and several heat exchangers and pumps. Such systems are known from the prior art and should therefore be described here only 21 * 9 200817716 in outline. In the absorber, the export gas to be cleaned 4 is introduced from below, while from above a acidic components of the gas absorbing solution, such as an amine solution flows down. Here, the CO 2 is now removed from the export gas 4 and the purified gas is fed to the reduction shaft 18 of the direct reduction plant 33.
    The loaded absorbent {the absorbent liquid) is passed from above into the stripper 9, where it is at> 100 ° C., in particular 110 °, with warm low-pressure steam 10 which has a temperature of approximately 120-260 ° C., in particular 150 ° C. -120 ° C, is heated, whereby the acidic gases, especially the CO 2, are released again as residual gas. The residual gas 11 can either be released into the atmosphere 15 again after an H2S purification 12 and / or, since it consists almost entirely of CO 2, a first compressor 13 for the compression of CO 2 to about 5-11 barg are fed to the compressed To use CO2 39 as a substitute for nitrogen in the production of pig iron in the COREX® process, in direct reduction or in synthesis gas production. When the compressed CO 2 is fed to the second compressor 38 for liquefaction of CO 2 after the first compressor 13 and liquefied, it may be diverted to store it approximately underground.
    In each case after each compressor 13, 38, a heat exchanger 40, 41 is provided, which extracts the heat supplied to the C02 in the compression. This heat may be used to regenerate the absorbent in the stripper 9.
    The resulting in the stripper 9 condensate 14 is withdrawn and can the steam cycle of a steam generating plant 34, that is about the steam boiler 16, are supplied.
    The export gas 4 can also be fed to the steam boiler 16 of a steam generating plant 34 as fuel via an export gas container 5. In addition, a blower 42 22 200817716 • »·» • ·
    Combustion air supplied. From the steam boiler 16, low-pressure steam 10 is removed and fed to the stripper 9. The low-pressure steam 10 may also be added to steam 35 from another waste heat boiler, for example from those waste heat boilers 6, 7 and / or 58 of the COREX® plant 32. Export gas not required for the steam boiler 16 can be used for other purposes, for example for drying raw materials 17 (FIG. Coal, fine or ore drying). The combustion exhaust gas of the steam generating plant 34 is passed through a flue pipe into the atmosphere.
    The COREX® plant 32 has in this example a reduction well 19, which is designed as a fixed bed reactor and is charged with lump, pellets, sinter and additives, see reference numeral 20.
    In countercurrent to the lump etc. 20, the reducing gas 21 is guided. It is introduced at the bottom of the reduction shaft 19 and exits at its top as a top gas 22. The heat of the top gas 22 from the reduction shaft 19 is used in a waste heat boiler 6 for generating steam, the resulting low-pressure steam is fed to the stripper 9 of the plant 1 for the chemical absorption of CO2. Before entering the waste heat boiler 6, the top gas 22 is freed of dust in a dust collector or cyclone 2.
    The exiting the waste heat boiler 6 exhaust gas is further purified in a wet scrubber 3 and as the export gas 4 as described above according to the invention the absorber 8 for C02 ~ removal supplied.
    The reducing gas 21 for the reduction shaft 19 is produced in a melter gasifier 23 into which coal in the form of lumped coal 24 and coal in powder form 25 - this together with oxygen 02 - is fed, in the other hand, the pre-reduced in the reduction shaft 19 iron ore added becomes.
    The coal in the melter gasifier 23 is gasified, resulting in a gas mixture consisting mainly of CO and H2, and 23 deducted as a top gas (generator gas) 26 and a partial stream 27 is fed as a reducing gas 21 the reduction shaft 19.
    The hot metal melted in the melter gasifier 23 and the slag are withdrawn, see arrow 27.
    The top gas 26 withdrawn from the melter gasifier 23 is first cooled in a waste heat boiler 58 and passed into a separator 28 to separate with discharged dust and return the dust 36 via dust burner in the melter gasifier 23.
    A portion of the top gas 26 purified by the coarse dust is further purified by means of wet scrubber 37 and removed as excess gas 29 from the COREX® plant 32 and, according to the invention, fed to the absorber 8 of the plant 1 for the chemical absorption of CO 2. Before the wet scrubber 37 or in the generator gas line 26, a further waste heat boiler 7, 58 may be arranged, the low-pressure steam is fed to the stripper 9.
    A portion of the purified top or generator gas 26 after wet scrubber 37 is fed to a gas compressor 30 for cooling and then fed back to the top or generator gas 26 after the melter gasifier 23 for cooling. As a result of this recycling, the reducing proportions contained therein can still be exploited for the COREX® process and, on the other hand, the required cooling of the hot top or generator gas 26 from about 10 ° C. to 700 ° -900 ° C. can be ensured.
    The stripper 9 can in this embodiment, on the one hand low-pressure steam 10 from the waste heat boilers 6, 7, 58 of the COREX® plant 32 and / or low-pressure steam from the steam boiler 16 of the steam generating plant 34 are supplied. Preferably, the waste heat from the iron production process or the direct reduction process should be used because of the short distances between «· · · ·« · «»
    200817716
    Waste heat boilers 6, 7, 58 and Appendix 1 for the chemical absorption of CO 2.
    The condensate 14 of the stripper 9 is supplied to the steam cycle of the steam generating plant 34 in this example. But it can also be the steam cycle of the waste heat boiler 6, 7 fed.
    If an oxygen blast furnace with top gas recirculation is used instead of the COREX® plant, the top or top gas is taken from the top of the blast furnace, a part is returned to the oxygen blast furnace and a part of the top or top gas is pre-cleaned in a dust separator or cyclone and a wet scrubber ( or a bag filter or hot gas filter system) cleaned again. The thus purified top or blast furnace gas is then removed directly as export gas 4 from the blast furnace system and fed to the plant 1 for the chemical absorption of CO 2.
    The released from C02 product gas from the absorber 8 is heated in a heating unit (reduction gas furnace) 43, which preferably has an air preheater 44, possibly partially oxidized with oxygen 02 and passed into the reduction shaft 18, where the abandoned from above lumpy ore and / or the pellets 45 are charged. The top gas 46 issuing from the reduction shaft 19 at the top is preferably dry-dedusted in a dust separator or cyclone 47 and cooled in a waste-heat boiler 48. The heat removed there from the top gas 46 can be used to regenerate the absorbent in the stripper 9.
    The top gas 46 is then further cleaned in a wet scrubber 49, compressed in a compressor 50 and cooled in a gas cooler 51, before it is added to the export gas 4 before the absorber 8. 25 • · 25 • · «« 200817716
    After the wet scrubber 49, a portion of the top gas 46 can be diverted and in turn a part of the export gas 4, which is passed as fuel via the export gas container 5 in the steam generating plant 34, are added.
    Another part may be supplied to the heating unit (reduction gas furnace) 43 as fuel. The heat from the reduction gas furnace 43 can be utilized in a waste heat boiler 59, which delivers the low pressure steam obtained thereby to the stripper 9 for regeneration of the absorbent.
    In the lower part of the reduction shaft 18, reducing gas is withdrawn as cooling gas 52, cooled in a waste heat boiler 53, cleaned in a wet scrubber 54, compressed in a compressor 55 and returned to the lower part of the reduction shaft 18. The steam generated in the waste heat boiler 53 can be used to regenerate the absorbent in the stripper 9.
    The reduction shaft 18 does not have to be a fixed bed, it can also be designed as a fluidized bed. At the lower end, either sponge iron, hot briquetted iron or low-iron iron 56 are removed, depending on the charged feedstock and depending on the process.
    The reduction duct 18 supplied export gas 4 need not be supplied entirely in the plant 1 for chemical absorption, a part can also be passed in a bypass line 57 to the plant 1 for chemical absorption around directly into the heating unit 43 and the product gas 31 before Heating unit 43 are mixed.
    If the heat is to be used for the regeneration of the absorption medium in the stripper 9 from an air separation plant, then a heat exchanger can be provided which is fed by one or two hot gas streams from an air separation plant: a gas stream comes from the main air compressor and has a pressure of about 4 -12 barg, in particular from about 200817716 26
    5 barg, and a temperature of about 280 ° C; a second gas stream comes from the booster air compressor and has a pressure of 5 to 25 barg, in particular of 23 barg, and a temperature of about 200 ° C. Alternatively, the heat exchange of hot air to an alternative heat transfer medium (for example, water / steam, thermal oil, nitrogen) and then from the heat transfer medium to the absorption liquid may also initially take place.
    4 shows the connection according to the invention between a plant for smelting reduction (namely a FINEX © plant 60), a direct reduction plant 33 with a plant 1 for the chemical absorption of CO 2 and a steam generating plant 34.
    The direct reduction plant 33 with the chemical absorption installation 1 and the steam generation installation 34 are essentially constructed as in FIG. 3.
    The export gas 4 of the FINEX © plant 60 can also be supplied via an export gas container 5 to the steam boiler 16 of the steam generating plant 34 as fuel. The low-pressure steam 10 can also be added to steam 35 from another waste heat boiler, for example from the waste heat boiler 61 of the FINEX® plant 60.
    The FINEX® plant has in this example four reduction reactors 62-65, which are formed as fluidized bed reactors and are charged with fine ore. Fine ore and additives 66 are supplied to the ore drying 67 and from there first to the fourth reactor 65, then they get into the third 64, the second 63 and finally the first reduction reactor 62. Instead of four fluidized bed reactors 62-65 but only three may be present , 200817716 27 I * 4 4 · · · I · · · ·
    In countercurrent to the fine ore, the reducing gas 68 is guided. It is introduced at the bottom of the first reduction reactor 62 and exits at the top. Before it enters from below into the second reduction reactor 63, it can still be heated with oxygen 02, as well as between the second 63 and third 64 reduction reactor. The heat of the exhaust gas 69 from the reduction reactors 62-65 is used in a waste heat boiler 61 for generating steam, the resulting low-pressure steam can be supplied to the stripper 9 of the plant 1 for the chemical absorption of CO2.
    The exhaust gas 69 leaving the fourth reduction reactor 65 is purified after the waste heat boiler 61 in a scrubber 70, before a partial flow is withdrawn as export gas 4 from the FINEX® plant 60. Another partial flow will be used as recirculation gas 71 again in the FINEX® process. To do this, it is compressed in the recycle gas compressor 72 and then fed to a pressure swing adsorption plant 73 where CO 2 is removed. A vacuum pressure swing adsorption unit or a chemical absorption could also be used.
    The residual gas stream 74 according to Appendix 73 contains mainly C02, a part of the residual gas can be supplied to the export gas 4 before entering the export gas container 5 for cooling, another part of the reduction gas furnace 43 for heating the product gas 31. The residual gas 74 could also in a separate , not shown here steam generator (waste heat boiler) heat to be withdrawn - optionally after mixing with export gas 4 - and used for the production of low-pressure steam for the stripper 9.
    The reducing gas 68 is in Fig. 4 in a
    Melt carburetor 75 produced in the one hand coal in the form of lumpy coal 76 and coal in powder form 77 - this together with oxygen 02 - is fed, in the other hand, the pre-reduced in the reduction reactors 62-65 and in the iron briquetting 78 in hot 200817716 28 * ··· · «♦ · · * * *
    Condition to briquettes (English: HCl Hot Compacted Iron) shaped iron ore is added. The iron briquettes arrive via a conveyor system in a storage tank 79, which is designed as a fixed bed reactor, where the iron briquettes with coarse purified gas generator 80 from the melter gasifier 75 optionally preheated and reduced. Cold iron briquettes 81 can also be added here. Subsequently, the iron briquettes or oxides are charged from above into the melter gasifier 75. Low reduced iron (LRI) may also be withdrawn from the iron briquetting 81.
    The coal in the melter gasifier 75 is gasified, resulting in a gas mixture consisting mainly of CO and H2, and withdrawn as a reducing gas (generator gas) 80 and a partial stream is fed as reducing gas 68 to the reduction reactors 62-65.
    The hot metal melted in the melter gasifier 75 and the slag are withdrawn, see arrow 82.
    The withdrawn from the melter gasifier 75 generator gas 80 is first passed into a separator 83 to deposit with discharged dust and return the dust on dust burners in the melter gasifier 75.
    A portion of the purified by the pulverized gas generator gas 80 is further purified by wet scrubber 84 and added to the export gas 4 as excess gas 85.
    Another part of the purified gas generator 80 is also further purified in a wet scrubber for cooling gas, fed to a gas compressor for cooling and then supplied to the generator gas 80 after the melter gasifier 75 for cooling after being mixed with the recirculated gas 71 removed from the system 73 , By virtue of this recirculation of the gas 71 freed from CO2, the reducing proportions contained therein can still be exploited for the FINEX © process and, on the other hand, the 200817716 29
    • · • t · · «> required cooling of the hot generator gas 80 must be ensured.
    The top gas leaving the storage tank 79, where the iron briquettes or iron oxides are heated and reduced with dedusted and cooled generator gas 80 from the melter gasifier 75, can be cleaned in a wet scrubber and then likewise fed to the plant 73 for removal of CO 2.
    In Fig. 5, the invention is illustrated by means of an oxygen blast furnace. Here, iron ore is supplied from a sintering plant 86 and coke (not shown) via a charging device from above into the blast furnace 87. Oxygen-containing gas 88 having an oxygen content > 80% is introduced into the loop of the blast furnace 87, as well as coal in powder form (not shown). In the reduction gas furnace 89, reducing gas 90 is heated, whereby oxygen 02 and combustion air are supplied for the combustion.
    Together with cold or preheated oxygen, the heated reducing gas 90 is introduced into the blast furnace 87. Slag and pig iron are drawn down from the blast furnace 87. In the upper part of the blast furnace 87, the top or top gas 91 is removed and pre-cleaned in a dust collector or cyclone and further purified in a wet scrubber 93. The purified top or top gas 91 is still so hot that its energy could be used in a waste heat boiler for steam generation and subsequently used for absorption in the system 1 (not shown).
    The waste heat from the reduction gas furnace 89 can also be utilized in a waste heat boiler 92 and then in the plant 1. As in the waste heat boilers of the other Fig. Here, the left circuit represents the steam cycle, the right circuit is used for heating and evaporation of condensate. 200817716 • · 30 • · «·· '« * * * · · · · · · * * β * * * ♦ ··' - «· ♦ · *« * «·« · ·· m
    The purified and optionally cooled top gas 91 can be partially removed directly as export gas 4 from the blast furnace system and fed to an optional expansion turbine 94 and then to the export gas container 5. Another part may be supplied to a pressure swing adsorption plant 73 for CO2 removal, wherein the purified and recirculating top or top gas 91 is previously cooled in a gas cooler cooled with cold water and then compressed with a compressor. In addition, in Fig. 5 a - dashed line shown - provided with which the top gas to be recycled 91 is passed to the system 73 past or gas cooler and system 73 as fuel gas in the reduction gas furnace 89.
    The product gas purified of CO2 is fed back to the blast furnace 87 as a reducing gas 91 either directly and / or after being heated in the reduction gas furnace 89. The rich CO2 residual gas 74 may be as shown in FIG. 4 partially fed as fuel gas to the reduction gas furnace 89. Finally, a portion of the residual gas 74 may be supplied to the export gas 4 for entry into the export gas container 5 (wherein, as explained in Fig. 4, a separate waste heat boiler for recovering low pressure steam could be arranged), another part of the reduction gas furnace 43 for heating the product gas 31.
    FIG. 6 shows the connection according to the invention between a coal gasification plant and a direct reduction plant. The direct reduction plant 33 with the chemical absorption installation 1 and the steam generation installation 34 are essentially constructed as in FIG. 3. There is only one more CC > 2 removal unit 04 after the gas cooler 51 for the top gas 46 from the reduction pit 18. 200817716 31
    ♦ · »« **
    The coal gasification plant consists of three sections: the left section shows the coal feed 95, with the coal being fed into the uppermost tank. The middle section shows the gasification 96 with the gasification reactor above and below the plant parts for sludge treatment. The right-hand area relates to the mechanical gas purification 97. Here, the gas is washed in the upper area, treated with low-pressure steam and then withdrawn as synthesis gas 98. In the lower part of the wash water from the gasification reactor is treated.
    In the gas aftertreatment 99, the CO fraction is reduced in the synthesis gas 98 on the one hand in a shift plant 100 by means of a water gas shift reaction, and on the other hand COS and HCN contained in the synthesis gas 98 are decomposed by hydrolysis in the hydrolysis plant 101. The heat of the thus purified synthesis gas 98 can be used in a waste heat boiler 102, the low-pressure steam of the system 1 can be fed to the regeneration of the absorbent. In addition, a cooler 103 may be provided for the synthesis gas 98 before it is fed to the plant 1. The synthesis gas could be deprived of energy by an expansion turbine 94 before entering the system 1.
    As already mentioned, the plant 1 for the chemical absorption of CO 2 could in each case also be replaced by a physical absorption, but this is economically and energetically meaningful only in the embodiment according to FIG. 6 due to the higher pressure of the synthesis gas.
    The plants of the rest of the metallurgical plant can be used as a source of steam or heat, such as heat from the converter gas cooling of the steel converter or from the electric arc furnace for steel production. 200817716 r
    LIST OF REFERENCES: 1 system for the chemical absorption of CO2 2 dust collector or cyclone 3 wet scrubber 4 export gas 5 export gas container 6 waste gas boiler for Topgas 22 7 aftercooler 8 absorber 9 stripper 10 low pressure steam 11 residual gas after stripper 9 12 H2S cleaning 13 first compressor for compression of C02 14 condensate 15 Atmosphere 16 Steam Boiler 17 For raw material drying (coal, fine coal or ore drying) 18 Reduction shaft of the direct reduction plant 19 Reduction shaft of the COREX® plant 20 lumps, pellets, sinters and additives 21 Reduction gas 22 Top gas from the reduction shaft 19 23 Melt carburetor 24 Lump coal 25 Coal in powder form 26 top or generator gas from melter gasifier 23 27 hot metal and slag 28 separator for fine ore 29 excess gas 30 gas compressor 31 gas freed of CO2 (product gas) from absorber 8 32 COREX® plant 33 direct reduction plant 34 steam generating plant 200817716 • · * ι »» · : 33 35 Steam from another Waste heat boiler 36 Dust from separator 28 37 Wet scrubber for Topgas 26 38 Second compressor for liquefying CO 2 39 compressed CO 2 as substitute for nitrogen 40 Heat exchanger after first compressor 13 41 Heat exchanger after second compressor 38 42 Blower for combustion air 43 Heating unit (reduction gas furnace) for product gas 31 44 Air preheater 45 pieces of ore and / or pellets 46 Topgas from reduction shaft 18 47 Dust separator or cyclone for Topgas 46 48 Waste gas boiler for Topgas 46 49 Wet scrubber for Topgas 46 50 Compressor for Topgas 46 51 Gas cooler for Topgas 46 52 Reduction gas as cooling gas from the lower part of the reduction shaft 18 53 Waste heat boiler for reducing gas 52 54 Wet scrubber for reducing gas 52 55 Compressor for reducing gas 52 56 Hot briquetted iron or low iron 57 Bypass pipe 58 Waste heat boiler for top or generator gas 26 59 Waste heat boiler for waste heat from reduction gas furnace 43 60 FINEX® unit 61 Waste heat Exhaust gas from reduction reactors 62-65 62 First reduction reactor 63 Second reduction reactor 64 Third reduction reactor 65 Fourth reduction reactor 66 Fine ore additives 67 Earthing 68 Reduction gas 69 Exhaust gas from reduction reactors 62-65 • 34 200817716 • »* ·« · 70 Exhaust gas scrubber 69 71 Recycle gas 72 recirculation gas compressor 73 pressure swing adsorption unit 74 residual gas 75 melter gasifier 76 lumped coal 77 coal in powder form 78 iron briquetting 79 storage tank 80 generator gas from melter gasifier 75 81 cold iron briquettes 82 hot metal and slag 83 separator 84 wet scrubber for generator gas 80 85 excess gas 86 sinter plant 87 blast furnace 88 Oxygen-containing gas 89 Reduction gas furnace 90 Reduction gas 91 Top or top gas 92 Heat recovery boiler for reduction gas furnace 89 93 Wet scrubber 94 De-energizing turbine 95 Coal feed 96 Gasification 97 Mechanical gas cleaning 98 Syn thesegas 99 Gas aftertreatment 100 Shift system 101 Hydrolysis system 102 Waste heat boiler 103 Cooler 104 Further C02 removal system
    权利要求:
    Claims (22)
    [1]
    200817716

    35 ι · · »·. 1. A method for removing CO2 from exhaust gases (4) of pig iron production plants or of synthesis gas plants, wherein the exhaust gases purified by CO 2 are subsequently used in a direct reduction plant (33), characterized in that from the exhaust gas (4) extracted from the process of pig iron production or synthesis gas production, before use in a direct reduction plant (33) the CO2 is removed by chemical absorption (1), the heat being at least partially provided for the regeneration of the absorbent, either by low pressure steam used from a steam turbine of a steam power plant and / or a steam turbine for utilizing the waste heat from pig iron production, and / or by low-pressure steam (10) from a waste heat boiler (16) of a steam power plant and / or from a waste heat boiler (6, 7, 58, 61, 92) for using the heat from the pig iron production and / or from a waste heat boiler (59) for utilizing the waste heat from the direct reduction plant (33), and / or from an air separation plant, and / or from process gases (22, 26, 29, 69) from plants for the production of pig iron, synthesis gas plants ( 98) 200817716 * * 36 · ι * · * * · ψ and / or from direct reduction plants {11, 46, 52).
    [2]
    2. The method according to claim 1, characterized in that is used as an absorbent potassium carbonate.
    [3]
    3. The method according to claim 1 or 2, characterized in that it comprises an amine wash.
    [4]
    4. The method according to claim 3, characterized in that primary amines, such as methylamine, monoethanolamine (MEA) and / or diglycolamine (DGA) are used.
    [5]
    5. The method according to claim 3 or 4, characterized in that secondary amines, such as diethanolamine (DEA) and / or diisopropanolamine (DIPA) are used.
    [6]
    6. The method of claim 3, 4 or 5, characterized in that tertiary amines, such as triethanolamine (TEA) and / or methyldiethanolamine (MDEA) are used.
    [7]
    7. The method of claim 3, 4, 5 or 6, characterized in that amino acid salts are used.
    [8]
    8. The method according to any one of claims 1 to 7, characterized in that top gas (91) from a blast furnace, in particular from an oxygen blast furnace (87) with Topgasrückführung, is purified by the CO2.
    [9]
    9. The method according to any one of claims 1 to 8, characterized in that the exhaust gas (22, 26, 29, 69} from a 200817716

    Smelting reduction plant and / or synthesis gas (98) of a synthesis gas plant is purified. 5
    [10]
    10. The method according to any one of claims 1 to 9, characterized in that at least one of the following process gases is used as process gas from plants for pig iron production: - Excess gas (29) from a smelting reduction plant, - Topgas (22, 69) from a smelting reduction plant or from a blast furnace, 10 - generator gas (26) from a smelting reduction plant - residual gas (74) from an installation (73) integrated into the plant for the production of pig iron for CO2 removal. 15
    [11]
    11. The method according to any one of claims 1 to 10, characterized in that the synthesis gas (98) is used as the process gas of synthesis gas plants.
    [12]
    12. The method according to any one of claims 1 to 11, characterized in that at least a portion of the top gas (46) is used as the process gas of direct reduction plants (33).
    [13]
    13. The method according to any one of claims 1 to 12, characterized in that heat is used for regeneration of the absorbent from a Luftzerlegungsanlage in the form of hot air from the main air compressor 20 or the booster air compressor or its waste heat via a heat transfer medium ,
    [14]
    14. The method according to any one of claims 1 to 13, characterized in that low-pressure steam is removed at the end of the expansion of the steam turbine.
    [15]
    15. The method according to any one of claims 1 to 14, characterized in that the obtained from the chemical absorption of CO2 rich gas (11) - optionally after compression (13) to 5-11 barg - as a substitute for nitrogen in the production of pig iron, in the Synthesis gas production, in which direct reduction and / or for the treatment and storage of C02 is used.
    [16]
    16. The method according to claim 15, characterized in that the heat generated during the compression (13) of the C02 rich gas (11) is used for the regeneration of the absorbent.
    [17]
    17. Device for carrying out the method according to one of claims 1 to 16, comprising a direct reduction plant (33) and a plant (1) for the removal of CO 2 by means of chemical absorption, characterized in that of the plant (1) for CO 2 deposition at least a line (31) leads to the reduction shaft (18) of the direct reduction plant (33) to subsequently use the exhaust gases purified by CO 2 in the direct reduction plant (33) and in the plant (1) for CO 2 deposition at least one line opens for exhaust gas (4), which was withdrawn from the process of pig iron production or syngas production, and wherein the plant part (9) for the regeneration of the absorbent - either connected to a steam turbine of a steam power plant or a steam turbine for using the waste heat from the pig iron production in that low-pressure steam from the steam turbine is at least partially fed into the plant part (9) for the regeneration of the Ab can be conducted sorbent, - and / or so with the waste heat boiler (16) of a steam power plant and / or the waste heat boiler (6, 7) for using the waste heat from the pig iron production and / or the waste heat boiler (59) to use the heat from the direct reduction plant (33) is connected that low-pressure steam can be used at least partially for the regeneration of the absorbent, - and / or connected to an air separation plant, that the heat from the air separation plant can be used at least partially for the regeneration of the absorbent, - and / or so with plants for the production of pig iron, synthesis gas plants and / or direct reduction plants are connected to heat from the process gases {11, 22, 26, 29, 46 , 52, 69, 98) of these systems can be used at least partially for the regeneration of the absorbent.
    [18]
    18. The apparatus according to claim 17, characterized in that in the plant (1} for CO 2 deposition at least one line opens for top gas (91) from a blast furnace, in particular from an oxygen blast furnace (87) with Topgasrückführung.
    [19]
    19. The apparatus of claim 17 or 18, characterized in that in the system (1) for 002 deposition at least one line opens for exhaust gas (22, 26, 29, 69) from a smelting reduction plant and / or synthesis gas (98) one synthesis gas plant.
    [20]
    20. Device according to one of claims 17 to 19, characterized in that for the use of heat from the process gases in the system part (9) for the regeneration of the absorbent of this with waste heat boilers (6, 7, 40, 41, 48, 53, 58, 61 , 102) for lines for - excess gas (29) from a smelting reduction plant, - top gas (22, 69) from a smelting reduction plant or from a blast furnace, - generator gas (26) from a smelting reduction plant, - synthesis gas (98) from a synthesis gas plant,

    200817716 - Topgas (46) from a direct reduction plant, - is connected.
    [21]
    21. Device according to one of claims 17 to 20, characterized in that the plant part (9) for the regeneration of the absorbent 5 is so connected to a Luftzerlegungsanlage that heat in the form of hot air from the main air compressor and / or the booster air compressor or its waste heat can be used via a heat transfer medium.
    [22]
    22. Device according to one of claims 17 to 21, characterized in that the plant part (9) for the regeneration of the absorbent so with a heat exchanger (40, 41) is connected to a compressor (13, 38) for compression of the CO2 rich gas 15 (11), that the heat from the compressed C02 rich gas can be used at least in part for the regeneration of the absorbent.
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    同族专利:
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    引用文献:
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    AT508770B1|2009-09-11|2011-04-15|Siemens Vai Metals Tech Gmbh|METHOD FOR REMOVING CO2 FROM EXHAUST GASES FROM PLANTS FOR THE PRODUCTION OF REFRIGERATED IRON|GB2509227B|2012-12-21|2015-03-18|Siemens Plc|A method for supplying blast to a blast furnace|
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    法律状态:
    2016-07-15| MM01| Lapse because of not paying annual fees|Effective date: 20151104 |
    优先权:
    申请号 | 申请日 | 专利标题
    ATA1819/2010A|AT510618B1|2010-11-04|2010-11-04|PROCESS FOR REMOVING CO2 FROM EXHAUST GASES|ATA1819/2010A| AT510618B1|2010-11-04|2010-11-04|PROCESS FOR REMOVING CO2 FROM EXHAUST GASES|
    PCT/EP2011/064861| WO2012059255A1|2010-11-04|2011-08-30|Method for removing co2 from exhaust gases|
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