WO2023203157A1 - Procédé et dispositif de combustion de matière première minérale carbonatée et procédé d'utilisation de gaz résiduaire et unité d'utilisation de gaz résiduaire pour celui-ci - Google Patents

Procédé et dispositif de combustion de matière première minérale carbonatée et procédé d'utilisation de gaz résiduaire et unité d'utilisation de gaz résiduaire pour celui-ci Download PDF

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Publication number
WO2023203157A1
WO2023203157A1 PCT/EP2023/060346 EP2023060346W WO2023203157A1 WO 2023203157 A1 WO2023203157 A1 WO 2023203157A1 EP 2023060346 W EP2023060346 W EP 2023060346W WO 2023203157 A1 WO2023203157 A1 WO 2023203157A1
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Prior art keywords
kiln
exhaust gas
raw material
furnace
gas
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PCT/EP2023/060346
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German (de)
English (en)
Inventor
Joachim Löffler
Sebastian Stephan GROPPWEIS
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Johann Bergmann Gmbh & Co
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Publication of WO2023203157A1 publication Critical patent/WO2023203157A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/84—Biological processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
    • C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/05—Preparation or purification of carbon not covered by groups C01B32/15, C01B32/20, C01B32/25, C01B32/30
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/364—Avoiding environmental pollution during cement-manufacturing
    • C04B7/367—Avoiding or minimising carbon dioxide emissions
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/12—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon dioxide with hydrogen
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N1/00—Microorganisms, e.g. protozoa; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
    • C12N1/20—Bacteria; Culture media therefor
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/202—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/208—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/95—Specific microorganisms
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B01D2256/245—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0233—Other waste gases from cement factories
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
    • C12P5/02—Preparation of hydrocarbons or halogenated hydrocarbons acyclic
    • C12P5/023—Methane

Definitions

  • the present invention relates to a method and a device for firing mineral, carbonate, granular or pourable raw material or firing material, in particular rock, preferably for firing limestone and/or magnesite and/or dolomite for producing quicklime and/or magnesia causter and /or sinter magnesia and/or doloma.
  • the invention also relates to an exhaust gas utilization method and an exhaust gas utilization device for it.
  • the invention preferably relates to a lime burning process and a device with a lime kiln for producing quicklime.
  • burning refers to various thermal processes in the production of materials and the production of semi-finished products.
  • firing is often used in the production of ceramic materials, powder metallurgy, and alcohol production. During firing, a chemical reaction or transformation of the crystal structure of a material is achieved by applying energy.
  • a granular material is a bulk material.
  • a bulk material is a dry mixture that consists of grains and is in a pourable form. If the grains are very fine, it is a powder or flour. In particular, a flour has a grain size ⁇ 400 pm. If the grains are also coarse, it is a lumpy (raw) material. In particular, a lumpy material also has grains with a grain size of > 5 mm.
  • the grain size is determined in particular in accordance with DIN 66165-1:2016-08.
  • the grain size is determined using air jet sieve analysis. If the raw material is lumpy, the grain size can also be measured using a caliper if the grain size is > 50 mm.
  • carbonate raw material consists predominantly (>50% by mass), preferably >70% by weight, particularly preferably >80% by mass, very particularly preferably >85% by weight, of the respective car - bonus(es).
  • a raw material that only contains carbonate impurities is not a carbonate raw material.
  • the composition is determined in particular in accordance with DIN EN 196-2:2013-10.
  • Quicklime or burnt lime (calcined CaO) is known to be produced by burning or calcining limestone (CaCOs) in a lime kiln. This process is known as lime burning. From a temperature of around 800 °C, calcium carbonate is deacidified, which means carbon dioxide is driven off and calcium oxide is formed:
  • doloma or caustic-fired dolomite or calcined dolomite (calcined CaO MgO) is created by firing or calcining dolomite stone (CaMg(CO3)2).
  • Magnesia (magnesia causter or caustic magnesia or causter magnesia and sinter magnesia) consists largely of magnesium oxide (MgO). It is mainly produced by thermal decarbonatization or deacidification of magnesite at temperatures of 600-800°C (magnesia causter) or 1800-2200°C (sintered magnesia). Natural magnesium carbonate (MgCOs) is called magnesite or raw magensite. The deacidification process of magnesite begins at approx. 550-800 °C, producing magnesia causter.
  • the magnesia causter is further thermally treated in one or two phases at 1800-2200 °C.
  • sintered magnesia can also be produced directly from the raw magnesite in a one-stage firing process.
  • the CO2 is separated from the exhaust gas. This is done, for example, through absorption or adsorption, Ca-based chemical looping using membranes or using the oxyfuel process.
  • the fuel is burned with pure oxygen (i.e. without nitrogen).
  • pure oxygen i.e. without nitrogen
  • the ideal case of stoichiometric combustion of a pure hydrocarbon with oxygen only CO2 and water are formed as combustion products.
  • the CO2 content is around 80% by volume. After the water has condensed out, only pure CO2 would remain. However, due to its high purity, this is only possible when using natural gas.
  • the EU-funded LEILAC 2 (Low Emissions Intensity Lime And Cement) project (https://cordis.europa.eu/proiect/id/884170/en) is testing a new technology that overhauls existing processes by directly heating the limestone .
  • This project builds on the successes of the Horizon 2020 project LEILAC (which managed to capture 5% of the CO2 process emissions of an average cement factory) and plans its output to approximately 20% of the CO2 process emissions with a deployable and scalable module. to scale up to an average cement factory.
  • EP 2 818 227 A1 discloses a method for operating a shaft kiln producing burnt lime, dolomite, magnesia or cement from carbonate-containing raw materials, in particular a method for operating a shaft kiln for producing burnt lime or cement, the shaft kiln having at least one upper raw material inlet zone , has at least one middle combustion zone and at least one lower combustion material outlet zone, characterized by the following measures: a) burning a fuel mixture made of a carbon-containing fuel, e.g. B.
  • a fossil fuel preferably methane or methanol, and industrially produced technical oxygen in the combustion zone of the shaft furnace and calcination of the carbonate-containing raw material in the combustion zone and above it, with additional carbon dioxide being added to the combustion zone and/or the outlet zone of the shaft furnace as a substitute the nitrogen-containing atmospheric air commonly used according to the prior art, b) removal of an exhaust gas containing at least 60, in particular at least 80, preferably over 90% by volume of carbon dioxide, resulting from the combustion of the fuel, e.g. B.
  • the methane or methanol with oxygen and the carbon dioxide supplied, at the inlet opening of the raw material inlet zone and introducing the exhaust gas into an exhaust gas storage, the carbon dioxide supplied according to feature a) being taken from the exhaust gas storage containing carbon dioxide, c) generating methane or methanol in a methanization or methanolization reactor from carbon dioxide supplied to the reactor from the exhaust gas storage and hydrogen supplied to the reactor and introducing the methane or methanol into a methane or methanol storage, d) supplying a carbon-containing e.g. B.
  • the object of the present invention is to provide a method and a device for firing mineral, carbonate-containing or carbonate.
  • Bonatical raw material or firing material preferably for firing limestone and/or magnesite and/or dolomite for the sustainable production of quicklime and/or magnesia causter and/or sintered magnesia and/or doloma.
  • FIG 1 Schematic and greatly simplified exhaust gas control according to the invention
  • Figure 2 Schematic and greatly simplified of a kiln with exhaust gas recirculation
  • Figure 3 Schematic and greatly simplified of a kiln with exhaust gas recirculation according to a further embodiment
  • Figure 4 Schematic and greatly simplified of a kiln with exhaust gas recirculation according to a further embodiment
  • Figure 5 Schematic and greatly simplified of a kiln with exhaust gas recirculation according to a further embodiment
  • FIG. 6 Schematic and greatly simplified of a kiln according to a further embodiment
  • the device 1 according to the invention (FIGS. 1, 2) has a combustion furnace 2, an exhaust gas recirculation device 3, an exhaust gas utilization device 4, a hot gas supply device 5 and a cooling gas supply device 6.
  • the device 1 according to the invention is preferably used to produce quicklime and/or magnesia causter and/or sintered magnesia and/or doloma from mineral, carbonate raw material or firing material, preferably by firing limestone and/or magnesite and/or dolomite.
  • the device 1 is preferably used to produce quicklime.
  • the kiln 2 is preferably a lime kiln.
  • the kiln 2 according to a first embodiment of the invention (FIG. 2) is a single-chamber shaft kiln or normal shaft kiln 7 with a single vertical kiln shaft 7a.
  • the kiln 2 in particular the normal shaft kiln 7, has an upper kiln end 2a, at which the raw material to be burned is fed, and a lower kiln end 2b, at which the burned, in particular calcined, material, preferably the quicklime, is removed from the kiln 2 , on.
  • the lower end of the furnace 2b is thus arranged downstream of the upper end of the furnace 2a in a vertical material transport direction 8.
  • the kiln 2, in particular the normal shaft kiln 7, also has, viewed in the material transport direction 8, a raw material lock 9, a preheating zone 10, a combustion zone 11, a cooling zone 12 and a discharge lock 13 for removing the burned material, in particular the quicklime, from the kiln 2 on.
  • the raw material lock 9 is thus arranged at the upper end of the furnace 2a and the discharge lock 13 is arranged at the lower end of the furnace 2b.
  • the normal shaft furnace 7 has, in a manner known per se, a furnace interior or furnace combustion chamber 14 and a furnace jacket surrounding it 15 on.
  • the furnace interior 14 is also sealed in a gas-tight manner in a manner known per se.
  • the raw material lock 9 serves in a manner known per se for introducing the raw material to be burned into the furnace shaft 7a in batches. It is designed in such a way that it can be closed in a gas-tight manner, especially after filling with the raw material.
  • the discharge lock 13 is used in a manner known per se to discharge the fired material in batches from the furnace shaft 7a. It is also designed in such a way that it can be closed gas-tight.
  • Relatively cool furnace process gas or cooling gas is also supplied at the lower end of the furnace 2b.
  • the cooling gas preferably has a temperature of -20 to 150 ° C, preferably 5 to 80 ° C.
  • the cooling gas is supplied at the lower end of the cooling zone 12.
  • the furnace exhaust gas is removed at the upper end of the furnace 2a.
  • the gas thus flows through the kiln 2 in a direction opposite to the material transport direction 8.
  • the kiln 2 is therefore operated in the countercurrent principle.
  • the kiln 2 is operated in a pure CO2 atmosphere.
  • the furnace process gas located in the furnace interior 14 has a CO2 content of >50% by mass, preferably >75% by mass, preferably >80% by mass, particularly preferably >90% by mass, very particularly preferred > 98% by weight.
  • the CO2 content of the gases is measured in a manner known per se using known measuring probes, preferably as part of a bypass measurement. This means that the measuring probe is arranged in a bypass.
  • the CO2 content in the furnace interior 14 does not have to be completely constant. However, it has the specified minimum CO2 content everywhere on. This is ensured by all furnace process gases introduced into the kiln 2 being >50% by mass, preferably >75% by mass, preferably >80% by mass, particularly preferably >90% by mass, very particularly preferably >98 M.-%, consist of CO2.
  • furnace process gases introduced do not contain any oxygen.
  • No combustion within the kiln 2 or in the kiln interior 14 means that no combustion takes place in which the kiln process gases located in the kiln 2 or in the kiln interior 14 react or are involved. Or no combustion takes place, which influences the oven atmosphere prevailing in the oven interior 14.
  • the kiln 2 therefore does not have a fuel heater with a burner for directly heating the raw material.
  • combustion can take place that is decoupled from the furnace atmosphere, for example in a space arranged in the furnace interior 14 but sealed off in a gas-tight manner from the furnace interior 14. This results in indirect heating of the raw material.
  • Electrical energy preferably from green electricity or green electricity, is also preferably, preferably exclusively, used to generate heat.
  • the heat necessary for firing the raw material is introduced into the firing zone 11 by supplying hot gas.
  • the hot gas is supplied at a hot gas inlet point 34 at the lower end of the combustion zone 11.
  • the hot gas is furnace process gas with the previous one stated high CO2 content.
  • the hot gas preferably has a temperature of 800 to 1,250 ° C, preferably 900 to 1,100 ° C.
  • the hot gas is heated in a hot gas heating device 16 of the heating gas supply device 5, which will be discussed in more detail below.
  • the pourable, lumpy raw material to be burned preferably the limestone
  • the raw material preferably has a minimum grain size >15 mm, preferably >30 mm, and/or a maximum grain size ⁇ 180 mm, preferably ⁇ 120 mm.
  • the purge gas is furnace process gas with the previously stated high CO2 content.
  • the purge gas preferably has an overpressure of 200 to 1800 mbar, preferably 200 to 800 mbar.
  • the device 1 preferably has a purge gas compression device 17.
  • the purge gas compression device 17 is preferably a rotary piston blower or a screw compressor or a hybrid blower, that is to say a combination of the two aforementioned blowers.
  • the purge gas preferably comes from a process gas storage device 22 or from gas bottles (not shown). However, it always has the previously stated high CO2 content.
  • the raw material lock 9 is flushed with the flushing gas until it is completely filled with it. Then the purge gas flow is switched off and the raw material lock 9 is opened to the furnace interior 14, so that raw material falls into the furnace interior 14, in particular into the preheating zone 10.
  • the connection between the raw material lock 9 and the furnace interior 14 is of course gas-tight. Because the raw material lock 9 is filled with the purging gas, no ambient air gets into the furnace interior 14.
  • the raw material is preheated in a manner known per se by the gas flowing from the combustion zone 11 and flowing counter to the material transport direction 8 through the preheating zone 10. This gas contains, on the one hand, the furnace process gases supplied and, on the other hand, the gases produced when the raw material is burned.
  • the raw material travels in countercurrent, namely in the material transport direction 8, through the preheating zone 10 and reaches the combustion zone 11.
  • the raw material is heated by the hot gas, which flows through the raw material against the material transport direction 8, in such a way that it is burned, in particular deacidified.
  • the material travels in countercurrent, namely in the material transport direction 8, through the combustion zone 11 and reaches the cooling zone 12.
  • the burned material is cooled by the cooling gas, which flows through the burned material counter to the material transport direction 8.
  • the cooled, fired material finally reaches the discharge lock 13, which discharges the material from the kiln 2.
  • the discharge lock 13 Before the discharge lock 13 is opened, it is separated in a gas-tight manner from the furnace interior 14 arranged above it so that no ambient air can penetrate into it.
  • the discharge lock 13 is flushed with flushing gas in the same way as the raw material lock 9 until it is completely is filled with this.
  • the purge gas flow is then switched off and the discharge lock 13 is opened to the furnace interior 14.
  • the connection between the discharge lock 13 and the furnace interior 14 is of course gas-tight.
  • the furnace exhaust gas is also discharged from the kiln 2 into the exhaust gas utilization device 4 at the upper end of the furnace 2a.
  • the furnace exhaust gas preferably has a temperature of 20 to 250 ° C, preferably 50 to 100 ° C.
  • the furnace exhaust gas is removed permanently or in batches, for example if a certain excess pressure, for example 600 mbar, is exceeded inside the furnace 14. This is regulated in particular via a pressure sensor and a valve controlled based on the measurements of the pressure sensor.
  • the furnace exhaust gas preferably has a CO2 content of >50 M%, preferably >75 M%, preferably >80 M%, particularly preferably >90 M%, very particularly preferably >98 M. -%, on.
  • the exhaust gas recirculation device 3 has, downstream of one another, preferably a first dedusting device 18, preferably a dehumidification device 19, preferably a second dedusting device 20, preferably an exhaust gas compression device 21 and the process gas storage device or exhaust gas storage device 22.
  • the first and second dust removal devices 18; 20 each serve to separate dust from the furnace exhaust gas.
  • the first dedusting device 18 preferably has one or more cyclones. Cyclones are also called centrifugal separators.
  • the second dedusting device 20 preferably has one or more filters, preferably filter bags.
  • the dehumidification device 19 is used to separate water and other moist components from the furnace exhaust gas. It is preferably a condensate drain, preferably with a refrigeration dryer.
  • the exhaust gas compression device 21 is used to compress the furnace exhaust gas. Compression serves to compensate for pressure losses.
  • the exhaust gas compression device 21 preferably has a screw compressor or a rotary piston blower or a hybrid blower or a pneumatic dynamic pressure compressor.
  • the exhaust gas storage device 22 serves to temporarily store the exhaust gas in a manner known per se.
  • the exhaust gas storage device 22 serves in particular as a system buffer.
  • the exhaust gas is preferably stored at approx. 1 bar.
  • an exhaust gas flow is discharged into the hot gas supply device 5, an exhaust gas flow into the cooling gas supply device 6 and an exhaust gas flow into the exhaust gas utilization device 4.
  • the hot gas supply device 5 has a hot gas compression device 23 and the hot gas heating device 16 connected thereto.
  • the hot gas compression device 23 serves to compress the gas discharged from the exhaust gas storage device 22 to in particular 200 to 1800 mbar, preferably 200 to 800 mbar. The compression serves to convey the hot gas through the furnace interior 14 with sufficient pressure.
  • the hot gas compression device 23 is preferably a screw compressor or a rotary piston blower or hybrid blower or a pneumatic dynamic pressure compressor.
  • the kiln 2 is preferably operated with excess pressure. This also serves to maintain the CO2 atmosphere in the furnace interior 14. Because This prevents gases from penetrating into the furnace interior 14 from outside.
  • the excess pressure in the furnace interior 14 is preferably 50 to 1200 mbar, preferably 200 to 800 mbar.
  • the gas then flows from the hot gas compression device 23 to the hot gas heating device 16.
  • the hot gas heating device 16 preferably has at least one electrically operated heater, preferably a resistance heater.
  • a resistance heater as is known, heat is generated by current flowing through a heating resistance element made of electrically conductive material and being heated by the Joule heat.
  • the resistance heater therefore has at least one heating resistance element around which the gas to be heated flows and heats it up.
  • the hot gas heating device 16 can also alternatively or additionally have at least one heat exchanger.
  • the heat exchanger has, in a manner known per se, one or more heat exchanger tubes through which a hot medium flows and the gas to be heated flows around them.
  • combustion preferably of natural gas or a fossil fuel, can take place in the heat exchanger tubes.
  • the hot gas heating device 16 serves to heat the gas to a temperature that is high enough to burn the raw material or to heat it to the necessary firing temperature.
  • the hot gas is generated, which is then introduced into the firing furnace 2, at the lower end of the firing zone 11.
  • the cooling gas supply device 6 has a cooling gas compression device 24 and an adjoining cooling gas cooling device 25.
  • the cooling gas compression device 24 serves to compress the gas discharged from the exhaust gas storage device 22 to in particular 200 to 1800 mbar, preferably 200 to 800 mbar. Compression serves to compensate for pressure losses.
  • the cooling gas compression device 24 is preferably a screw compressor or a rotary piston blower or a hybrid blower or a pneumatic dynamic pressure compressor.
  • the gas then flows from the cooling gas compression device 24 to the cooling gas cooling device 25.
  • the cooling gas cooling device 25 serves to cool the compressed gas, in particular to -20 to 150 ° C.
  • the cooling gas cooling device 25 preferably has at least one heat exchanger. By means of the cooling gas cooling device 25, the cooling gas is made available, which is then introduced into the kiln 2, at the lower end of the cooling zone 12.
  • the exhaust gas utilization device 4 has a methanation device 26, a methane pyrolysis device 27 and, if necessary, an electrolysis device 28 and, if necessary, a gas purification device 29.
  • the exhaust gas utilization device 4 preferably has a high-pressure compressor 46, a high-pressure accumulator 47 and a pressure reducer 48 in front of the methanation device 26.
  • the pressure reducer serves to reduce the pressure exactly to the pressure required for the methanation device 26.
  • the gas purification device 29 which is arranged in front of the methanation device 26, serves to purify exhaust gases and in particular ensures that no oxygen gets into the methanation device 26. In particular, it separates the CO2 from the other components, especially the oxygen, of the furnace exhaust gas.
  • the gas cleaning device 29 preferably has at least one membrane filter in a manner known per se.
  • the methanation device 26 is used to convert the CO2 into methane (CH4).
  • the methanation device 26 preferably has means for methanogenesis or microbial methane formation or biological methane formation.
  • methane is formed through the metabolism of living organisms called methanogens or methane producers.
  • the methane producers are preferably archaea.
  • Methanogenesis is carried out in a bioreactor with the help of methane producers, preferably archaea.
  • the methanation device 26 preferably has at least one bioreactor with archaea.
  • the bioreactor is also preferably operated at excess pressure, preferably at a pressure of 1 to 100 bar, particularly preferably 10 to 35 bar, very particularly preferably 10 to 20 bar.
  • the methanation device 26 can also alternatively or additionally have means for technical or chemical methanation.
  • the methanation device 26 has at least one membrane reactor for this purpose.
  • methanogenesis is preferred.
  • the hydrogen used for methanation now comes at least partially from the methane pyrolysis device 27.
  • the methane pyrolysis device 27 serves to convert the methane produced in the methanation device 26 into hydrogen and solid carbon.
  • Turquoise hydrogen Methane pyrolysis requires thermal energy, which can be generated using electricity. The power consumption is significantly lower than with electrolysis.
  • the methane is converted according to the following equation:
  • the methane pyrolysis device 27 preferably has at least one liquid metal bubble column reactor filled with molten metal, preferably with molten tin.
  • the methane gas is introduced at the bottom of the reactor and released there in the form of bubbles. Due to the difference in density, the bubbles rise upwards and represent a kind of micro-reactor chamber for the splitting during pyrolysis. Due to the hot metal, the methane quickly reaches the required reaction temperature, so that the splitting takes place while the bubbles are rising. The released carbon is deposited on the surface of the bubble. When the bubbles reach the top of the liquid metal reactor, they burst and release a mixture of hydrogen, carbon and, if necessary, residual methane. The solid carbon is then separated from the gas mixture. And the hydrogen produced is separated using a gas separation process, so that two reaction products are ultimately present individually. The residual methane is added again to the pyrolysis circuit of the liquid metal bubble column reactor.
  • the methane pyrolysis device 27 can also have means for carrying out the methane pyrolysis using the Kvaerner process.
  • the Kvaerner process as is known, the hydrocarbons are separated into pure carbon and hydrogen in a plasma torch at around 1600 °C.
  • the methane pyrolysis device 27 can also be supplied with natural gas, in particular from a pipeline or a natural gas storage facility, in addition to the methane coming from the methanation device 26.
  • the exhaust gas utilization device 4 can also additionally have the electrolysis device 28. This serves to provide additional hydrogen for methanation.
  • hydrogen is produced from water according to the following equation:
  • the additional hydrogen for methanation can also be provided from a hydrogen storage and/or a hydrogen network.
  • the additional hydrogen can also be provided using the LOHC process (liquid organic hydrogen carrier).
  • LOHC process liquid organic hydrogen carrier
  • the advantage of the method according to the invention and the device 1 according to the invention with the exhaust gas utilization device 4 according to the invention is that the CO2 produced during combustion does not reach the atmosphere, but is first converted into methane in the methanation device 26, which in turn is converted into solid carbon by methane pyrolysis becomes. Unlike carbon dioxide, solid carbon is not harmful to the climate and can be used, for example, as fertilizer.
  • methane pyrolysis Another advantage of methane pyrolysis is that it requires 80% less energy than electrolysis. This in turn also saves costs.
  • Half of the hydrogen used in the methanation device 26 is also recovered through methane pyrolysis.
  • the kiln exhaust gas is much purer and has hardly any impurities, so that exhaust gas cleaning can be dispensed with. If necessary, exhaust gas cleaning only needs to be carried out if the impurities have accumulated in the furnace exhaust gas. It is particularly important for the bioreactor that the furnace exhaust gas to be methanized contains few impurities, as archaea are sensitive in this regard. The possible elimination of exhaust gas cleaning also saves energy and costs.
  • archaea Another advantage of archaea is that although they are sensitive to oxygen in the exhaust gas, they are insensitive to high sulfur content in the exhaust gas.
  • the entire energy that is necessary to operate the device 1, in particular the kiln 2 and the exhaust gas utilization device 4 is preferably electrical energy, preferably from green electricity, the entire device 1 is almost climate-neutral.
  • the efficiency of the kiln 2 can be increased by operating exclusively in a CO2 atmosphere, since the dew point temperature can be reduced, which in turn can save energy.
  • water vapor is created.
  • the fuel often contains sulfur, which forms sulfuric acid with the water, causing the stove to corrode. Without the combustion of fuel inside the furnace, these problems do not occur.
  • the operation of the kiln 2 described above naturally refers to the normal operation of the kiln 2.
  • the kiln 2 is operated as described above until the desired CO2 concentration is achieved through concentration.
  • the exhaust gas utilization device 4 be put into operation. Beforehand, the excess exhaust gas is released into the atmosphere.
  • the furnace interior 14 can be flushed with flushing gas with the desired CO2 concentration before being put into operation.
  • the purge gas comes, for example, from the exhaust gas storage device 22 or gas bottles.
  • the firing furnace 2 has a firing material heating device 30, preferably arranged in the furnace interior 14, for heating the raw material or firing material in the firing zone 11 to the temperature necessary for firing.
  • the firing material heating device 30 generates the heat without burning fuel in the furnace interior 14.
  • the firing material heating device 30 does not have a fuel heater with a burner for directly heating the raw material.
  • the firing material heating device 30 is preferably arranged at the upper end of the firing zone 11.
  • the firing material heating device 30 is preferably operated electrically. So it has at least one electrically operated heater.
  • the firing material heating device 30 preferably has at least one resistance heater.
  • the resistance heater preferably has at least one, preferably several, electrical heating resistance element(s) 31, preferably heating rods or heating coils.
  • the heating resistance elements 31 are arranged in the furnace interior 14 or protrude into it.
  • the heating resistance element(s) 31 protrude into the raw material bed located in the furnace interior 14.
  • several heating resistance elements 31 can be arranged next to one another and/or one above the other.
  • the heating resistance elements 31 can also be distributed over the entire combustion zone 11.
  • the firing material heating device 30 can also have at least one heat exchanger (not shown).
  • several heat exchangers can be arranged next to one another and/or one above the other.
  • the heat exchangers can also be used the entire combustion zone 11 be distributed.
  • the heat divers are also preferably mechanically protected from the flow of raw materials.
  • a heat exchanger has, in a manner known per se, one or more heat exchanger tubes through which a hot medium flows and the raw material to be heated and the furnace process gas flow around them.
  • combustion of natural gas or a fossil fuel can take place in the heat exchanger tubes (indirect heating of the raw material).
  • at least one solid oxide fuel cell (SOFC) can be arranged in the heat exchanger tubes.
  • the electrically operated firing material heating device 30 can also have at least one microwave heater, which has means for heating the raw material by means of microwaves, and / or at least one arc heater with an anode and cathode arranged in the furnace interior 14.
  • the furnace exhaust gas is not contaminated by gases and unburned oxygen produced during combustion.
  • firing material heating device 30 for heating the firing material and to dispense with the introduction of the hot gas into the firing zone 11.
  • the kiln 2 is an inclined shaft kiln 33 (FIG. 4).
  • the inclined shaft furnace 33 is also operated in a manner known per se using the countercurrent principle.
  • the inclined shaft furnace 33 has, in a manner known per se, a combustion zone 11 with a plurality of combustion zone regions 11a-d arranged one above the other.
  • the firing zone areas are also designed in such a way that the firing material passes through the firing zone 11 on a meandering path.
  • the furnace shaft 33a is thus designed to be meandering in the area of the firing zone 11.
  • each combustion zone region 11 ad preferably has a hot gas inlet point 34 for introducing hot gas. This means that the material to be fired is heated optimally.
  • the hot gas inlet points 34 of the combustion zone regions 11 a-d arranged directly one above the other are preferably opposite each other. This means that there are always two hot gas inlet points 34 one above the other. This is particularly due to space reasons.
  • the hot gas supply device 5 preferably also has a hot gas compression device 23 and two hot gas heating devices 16 each adjoining the hot gas compression device 23. And two hot gas streams are removed from each of the hot gas heating devices 16 and introduced into one of the combustion zone areas 11 a-d.
  • the firing zone areas 11a-d have a firing material heating device 30 (not shown) in addition to or as an alternative to the hot gas inlet points 34.
  • part of the firing zone areas 11a-d can also have a firing material heating device 30 and part can have a hot gas inlet point 34.
  • the heating resistance elements or anode and cathode are preferably arranged in such a way that they are arranged in the furnace interior 14 but outside the raw material bed. This also applies to the heat exchanger tubes. This significantly reduces the mechanical wear of the respective heating elements.
  • the advantage of the inclined shaft furnace 33 is a more even heat and energy distribution. This ensures a better opportunity to influence the quality of the fired material.
  • the kiln 2 is a floating shaft kiln 35 (FIG. 5).
  • the floating shaft furnace 35 also has a single vertical furnace shaft 35a.
  • the floating shaft kiln 35 is operated on the direct current principle.
  • the material transport direction 8 corresponds to the flow direction of the furnace process gas.
  • the material transport direction 8 runs from bottom to top. The material outlet is therefore at the upper end of the oven 2a.
  • the floating shaft kiln 35 is not used for firing lumpy raw material, but rather floury raw material, preferably limestone powder.
  • the flour-like raw material has a grain size ⁇ 400 pm, preferably ⁇ 200 pm, preferably ⁇ 90 pm.
  • the firing material in the floating shaft furnace 35 is dispersed in the furnace process gas or floats in the floating shaft furnace 35.
  • the firing material is therefore transported through the floating shaft furnace 35 by means of the furnace process gas.
  • the device 1 also has an exhaust gas recirculation device 3, an exhaust gas recycling device 4 and a hot gas supply device 5.
  • the floating shaft furnace 35 has a hot gas distribution device 36, a combustion zone 37 and a recuperation zone 38.
  • the floating shaft furnace 35 has a raw material lock 39 and a raw material inlet point 49, which is arranged above the hot gas distribution device 36 and below the combustion zone 37 and next to the furnace shaft 35a.
  • the combustion zone 37 also has one or more, preferably up to 30, combustion zone regions 42 arranged one behind the other in the material transport direction 8.
  • the firing zone areas 42 each have a firing material heating device 43.
  • the firing material heating device 43 preferably has at least one electrically operated heater, preferably an arc heater or a resistance heater or a microwave heater, and/or at least one heat exchanger. Analogous to the other kilns 2; 7; 33, the heating resistance elements 31 of the resistance heater or the anode and cathode or the heat exchanger tubes are arranged in the furnace interior 14.
  • hot gas is conveyed into the hot gas distribution device 36 at the lower end of the furnace 2b at the hot gas inlet point 34 into the furnace shaft 35a.
  • the hot gas is previously heated in the hot gas heating device 16, preferably to 300 to 800 ° C, preferably 550 to 750 ° C.
  • the hot gas supply device 5 preferably also has a conveyor fan 50 arranged in front of the hot gas heating device 16.
  • the pourable, powdery raw material to be burned preferably the limestone powder, is filled into the raw material lock 39.
  • the raw material lock 39 As soon as the raw material lock 39 is filled, it is sealed gas-tight and flushed with flushing gas (not shown).
  • the purge gas preferably has an excess pressure of 200 to 1800 mbar.
  • the device 1 preferably has a purge gas compression device 17 (not shown in FIG. 5).
  • the purge gas compression device 17 is preferably a rotary piston blower or a screw compressor or a hybrid blower or a pneumatic dynamic pressure compressor.
  • the raw material lock 39 is flushed with the flushing gas until it is completely filled with it. Then the purge gas flow is switched off and the raw material lock 39 is opened to the furnace interior 14 so that raw material can be conveyed into the furnace interior 14.
  • a preheating device 41 is preferably arranged between the raw material lock 39 and the furnace interior 14, which serves to preheat the raw material before it is placed in the furnace interior 14.
  • the raw material is preheated to 300 to 800°C.
  • the preheating device 41 is preferably electrically operated and preferably has at least one electrical heater, preferably a resistance heater. But it can also alternatively or additionally have a heat exchanger.
  • the preheating device 41 can also have at least one microwave heater.
  • the raw material enters the firing zone 37, is transported through it and burned in the process.
  • the burned material enters the recuperation zone 38, in which it cools down by releasing the thermal energy to a heat exchanger or to a heat storage device, which in turn is used to preheat the raw material.
  • the burned material is discharged from the recuperation zone 38 into the exhaust gas recirculation device 3 together with the furnace exhaust gas in which it is dispersed.
  • the furnace exhaust gas is separated from the burned, dusty material.
  • the furnace exhaust gas is then conveyed into the exhaust gas storage device 22 as described above and from there into the hot gas supply device 5 and the exhaust gas utilization device 4 according to the invention.
  • the burned material separated in the first dedusting device 18 is preferably viewed in a sifting device 44.
  • completely burned, in particular completely calcined, material is separated from not completely burned, in particular not completely calcined, material.
  • the sifting device 44 has an air classifier which separates heavy unfired material from lighter fired material by forcing light fired material outwards by air, for example, and heavy fired material falling down without being deflected.
  • the incompletely burned material is then fed to the raw material lock 39 together with the raw material.
  • the completely burned material is preferably conveyed into a storage device 45.
  • the advantage of the floating shaft furnace 35 is the use of extremely fine material; there is practically no inevitable accumulation of undersized particles. Besides, can The floating shaft furnace can be started up and shut down much more quickly than conventional furnaces.
  • the kiln 2 is also a normal shaft kiln 7 (FIG. 6).
  • the normal shaft furnace 7 has a raw material feed device 51, the raw material lock 9, optionally the preheating zone 10, the combustion zone 11, the cooling zone 12 and the discharge lock 13.
  • the device 1 has the exhaust gas evaluation device 4 and the hot gas supply device 5, but preferably no cooling gas supply device 6.
  • the raw material feed device 51 serves to feed the raw material to the raw material lock 9. It preferably has a feed screw 51a, preferably a trough screw, with a heat exchanger. This preheats the raw material in the feed screw 51a.
  • the heat exchanger of the feed screw 51a preferably has heat exchanger tubes (not shown) arranged around the outside of a screw wall of the feed screw 51a, through which a heat exchange medium, preferably thermal oil, flows.
  • the feed screw 51a can also have an electric heater with at least one heating coil arranged around the screw wall of the feed screw 51a.
  • the raw material lock 9 has an upper and a lower pendulum flap 52a; 52b.
  • the two pendulum flaps 52a; 52b have an open and a closed position. In the closed position, they close the raw material lock 9.
  • the raw material lock 9 can be filled with raw material from above using the raw material feed device 51.
  • the lower pendulum flap 52c is open, the raw material falls from the raw material lock 9 into the furnace interior 14, in particular special the preheating zone 10.
  • the normal shaft furnace 7 has corresponding drive means, preferably hydraulic and/or pneumatic drive means and/or an electric motor and/or a servo motor.
  • the normal shaft furnace 7 also has an electrically operated firing material heating device 53 for heating the raw material or firing material in the firing zone 11 to the temperature necessary for firing.
  • the firing material heating device 53 has two resistance heaters in the form of heating sleeves 54 for each firing zone 11a-d, which are arranged on the outside around the furnace jacket 15, which is preferably made of steel.
  • the heating sleeves 54 each have an inner heating shell 55, an insulating shell 56 arranged around the outside of the heating shell 55 and preferably an outer sleeve shell 57 arranged around the outside of the insulating shell 56.
  • the heating shells 55 each have at least one electrical heating resistance element, preferably at least one heating coil, preferably several heating coils (not shown).
  • the furnace jacket 15 is thus heated by means of the heating jackets 54 and the heat generated by the heating jackets 54 is transferred through the furnace jacket 15 into the furnace interior 14 by means of heat conduction.
  • the hot gas supply device 5 preferably has a hot gas circulation device or furnace exhaust gas circulation device 58, the first dedusting device 18, a heat exchanger 59 for cooling the exhaust gas, a throttle 60, the exhaust gas compression device 21, the exhaust gas storage device 22 and a further throttle 61.
  • the hot gas circulation device or furnace exhaust gas circulation device 58 serves to circulate a portion of the hot furnace exhaust gas emerging from the combustion zone 11 at the upper end.
  • the hot gas circulation device 58 serves to remove the hot furnace exhaust gas at the upper end of the combustion zone 11 and to return the hot furnace exhaust gas to the lower end of the combustion zone 11.
  • the hot gas circulation device 58 has corresponding hot gas lines and at least one hot gas drive device or furnace exhaust gas drive device 62 for accelerating the hot gas or .Oven exhaust gas.
  • the hot gas drive device 62 is preferably a Coanda nozzle 63 or a high-temperature blower (not shown).
  • the heat exchanger 59 serves to cool the exhaust gas and has, for example, thermal oil as the heat exchange medium.
  • the heated thermal oil from the heat exchanger 59 can be used, for example, for the feed screw 51a.
  • the cooling zone 12 preferably has a cooling screw 64, which is preferably designed as a trough screw and has a closed, circumferential screw wall 64a.
  • the cooling screw 64 has a heat exchanger and thus means for dissipating the heat of the fired, in particular calcined, material.
  • the heat exchanger of the cooling screw 64 preferably has heat exchanger tubes (not shown) arranged around the outside of a screw wall of the cooling screw 64, through which a heat exchange medium, preferably thermal oil, flows.
  • the heated thermal oil can be used, for example, for the feed screw 51a.
  • no cooling gas is introduced into the cooling zone 12.
  • the cooling screw 64 has a cooling screw drive motor 65 in a manner known per se.
  • the discharge lock 13 adjoins the cooling zone 12.
  • the discharge lock 13 also has two pendulum flaps 66a; b for opening and closing the discharge lock 13.
  • the raw material to be burned is first weighed and added in batches to the raw material feed device 51, in particular the screw conveyor 51a, until it is filled. Then the screw conveyor 51a is started and the raw material is filled into the raw material lock 9.
  • the upper pendulum flap 52a of the raw material lock 9 is open, the lower pendulum flap 52b of the raw material lock 9 is closed.
  • the entire firing process is a discontinuous process.
  • the upper pendulum flap 52a is closed and the raw material lock 9 is flushed with flushing gas as described above.
  • the raw material lock 9 is flushed with the flushing gas until it is completely filled with it.
  • the flushing gas flow is switched off and the raw material lock 9 is opened to the furnace interior 14 by opening the lower pendulum flap 52b of the raw material lock 9.
  • the raw material falls into the furnace interior 14, in particular into the preheating zone 10.
  • the raw material travels in countercurrent, namely in the material transport direction 8, through the furnace interior 14 and reaches the firing zone 11.
  • the raw material is heated by the hot gas, which flows through the raw material against the material transport direction 8, as described above, in such a way that it is burned, in particular deacidified.
  • the material travels in countercurrent, namely in the material transport direction 8, through the combustion zone 11 and reaches the cooling zone 12.
  • the hot gas is not heated in a hot gas heating device 16 outside the furnace interior 14, but rather it is heated inside the furnace interior 14, during which the combustion zone 11 flows against the material transport direction 8.
  • the hot gas is heated by means of the firing material heating device 53.
  • the furnace jacket 15 is heated by means of the heating sleeves 54 and the hot gas flowing along it is heated.
  • This embodiment is particularly advantageous because no heating elements are arranged in the furnace interior 14 and hinder the flow of material.
  • a hot gas heating device is present if this is necessary.
  • the hot gas or the furnace exhaust gas is also circulated by means of the hot gas circulation device 58:
  • the furnace exhaust gas is removed from the furnace interior 14 at the upper end of the combustion zone 11.
  • a first exhaust gas stream is supplied to the exhaust gas storage device 22 via the dedusting device 18, the heat exchanger 59, the throttle 60 and the exhaust gas compression device 21, as described above.
  • a further exhaust gas stream of the furnace exhaust gas, the circulating hot gas, is fed to the hot gas drive device 62, preferably the Coanda nozzle 63.
  • the ratio of the first exhaust gas stream/hot circulating gas is 1:5 to 1:10.
  • the circulating hot gas is preferably not dedusted, but is fed directly to the hot gas drive device 62, preferably the Coanda nozzle 63. In particular, it is not temporarily stored in the exhaust gas storage 22.
  • the circulating hot gas is accelerated and then returned to the furnace interior 14 below the combustion zone 11.
  • the circulating hot gas is accelerated in the Coanda nozzle 63 in a manner known per se by means of a drive gas, which is also supplied to the Coanda nozzle 63.
  • the drive gas is also furnace exhaust gas, which is removed from the exhaust gas storage device 22 and fed to the Coanda nozzle.
  • the drive gas and the circulating hot gas mix in a manner known per se in the Coanda nozzle and are then returned to the furnace interior 14 below the combustion zone 11 and flow through the combustion zone 11 from bottom to top as described above.
  • Coanda nozzle 63 is particularly advantageous because it is wear-free.
  • the cooling zone 12 with the cooling screw 64 adjoins the combustion zone 11.
  • the cooling screw 64 is preferably also operated discontinuously. The fired material is thereby transported through the cooling screw 64 and thereby cooled, in particular by means of the thermal oil.
  • the fired material enters the discharge lock 13.
  • the upper pendulum flap 66a of the discharge lock 13 is opened and the lower pendulum flap 66b of the discharge lock 13 is closed.
  • the upper pendulum flap 66a of the discharge lock 13 is closed and then the lower pendulum flap 66b of the discharge lock 13 is opened and the fired material is discharged from the kiln 2.
  • the discharge lock 13 is flushed with flushing gas, similar to the raw material lock 9, as also described above, until it is completely filled with it.
  • kiln exhaust gas from the kiln 2 at various points.
  • the furnace exhaust gas which is supplied to the exhaust gas storage device 22, can be removed at a different location, for example further up, than the furnace exhaust gas for the hot gas circulation device.
  • a circulation device for circulating the exhaust gas can also be present above the combustion zone 11. This circulating gas is then used to preheat the raw material.
  • the exhaust gas utilization device 4 for the utilization of the exhaust gas from a kiln 2 which is conventionally operated with the combustion of fuels in the interior of the furnace 14.
  • combustion can also take place using the oxyfuel process.
  • the exhaust gas utilization device 4 can be used for other types of industrial kiln, e.g. for a rotary kiln or a tunnel kiln or other shaft kilns, preferably a GGR kiln (direct current countercurrent regenerative kiln) or a ring shaft kiln, or a push table kiln.
  • a GGR kiln direct current countercurrent regenerative kiln
  • ring shaft kiln a ring shaft kiln
  • push table kiln e.g. for a rotary kiln or a tunnel kiln or other shaft kilns
  • the industrial kilns are used for industrial firing/deacidification in contrast to small-volume laboratory kilns, which are used for experimental purposes.
  • the exhaust gas utilization device 4 can preferably be part of a device for producing cement clinker.
  • carbonate raw material in particular limestone and/or marl, is calcined or deacidified.
  • such a device either has an upstream kiln (calcining kiln) or the calcination or deacidification takes place in the same kiln in which the sintering to form cement clinker takes place.
  • another conversion device for converting CO2 and preferably hydrogen into other hydrocarbons or alcohol can be present.
  • This can also be done by converting CO2 into CO.
  • a conversion into propane and/or butane and/or propene and/or butene and/or methanol (methanolization device) and/or synthetic fuels and/or synthetic motor oils takes place.
  • the conversion into synthetic fuels and/or engine oils is preferably carried out using Fischer-Tropsch synthesis.

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Abstract

L'invention concerne une unité d'utilisation de gaz résiduaire (4) pour l'utilisation de gaz résiduaire contenant du CO2, en particulier une unité d'utilisation de gaz résiduaire (4) pour des gaz résiduaires de four provenant de fours (2) pour mettre en œuvre une combustion d'une matière première carbonatée, de préférence du calcaire et/ou de la magnésite et/ou de la dolomite et/ou de la marne, comprenant une unité de méthanation (26) pour convertir le CO2 contenu dans les gaz résiduaires en méthane et en eau avec l'ajout d'hydrogène, une unité de pyrolyse de méthane (27) pour convertir le méthane produit dans l'unité de méthanation (26) en hydrogène et en carbone solide, et un moyen pour transporter l'hydrogène produit dans l'unité de pyrolyse de méthane (27) dans l'unité de méthanation (26), ainsi qu'un procédé d'utilisation de gaz résiduaire correspondant. L'invention concerne également un dispositif et un procédé de combustion de matière première carbonatée fluide, de préférence du calcaire et/ou de la magnésite et/ou de la dolomite et/ou de la marne, avec une unité d'utilisation de gaz résiduaire de ce type ou un procédé d'utilisation de gaz résiduaire de ce type.
PCT/EP2023/060346 2022-04-20 2023-04-20 Procédé et dispositif de combustion de matière première minérale carbonatée et procédé d'utilisation de gaz résiduaire et unité d'utilisation de gaz résiduaire pour celui-ci WO2023203157A1 (fr)

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DE102022203882.7 2022-04-20
DE102022203882.7A DE102022203882A1 (de) 2022-04-20 2022-04-20 Verfahren und Vorrichtung zum Brennen von mineralischem, carbonatischem Rohmaterial sowie Abgasverwertungsverfahren und Abgasverwertungseinrichtung dafür

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WO2018192267A1 (fr) * 2017-04-17 2018-10-25 王长春 Dispositif de four à chaux pour la récupération complète de co2
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DE102016219990B4 (de) 2016-10-13 2018-05-30 Marek Fulde Verfahren zur Abscheidung und Lagerung von Kohlendioxid und/oder Kohlenmonoxid aus einem Abgas
WO2018099709A1 (fr) 2016-11-29 2018-06-07 Climeworks Ag Procédés d'élimination de co2 de l'air atmosphérique ou d'un autre gaz contenant du co2 afin d'obtenir des réductions d'émissions de co2 ou des émissions de co2 négatives

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DE102010019330A1 (de) 2010-05-05 2011-11-10 Ecoloop Gmbh Verfahren zur Umwandlung von Carbonaten in Oxide
EP2818227A1 (fr) 2013-06-28 2014-12-31 Fels-Werke GmbH Procédé d'opération d'un four droit produisant de la chaux, du dolomite, de la magnésie ou du ciment brûlés et installation de four droit destinée à la production de la chaux, du dolomite, de la magnésie ou du ciment brûlés
JP2015196619A (ja) * 2014-04-01 2015-11-09 株式会社Ihi 二酸化炭素固定システム
US20170314045A1 (en) * 2014-12-30 2017-11-02 Usw Commercial Services Ltd Microbial processing of gases
EP3156519A1 (fr) * 2015-10-16 2017-04-19 Volkswagen Aktiengesellschaft Procédé et appareil de production d'un hydrocarbure
WO2018192267A1 (fr) * 2017-04-17 2018-10-25 王长春 Dispositif de four à chaux pour la récupération complète de co2
KR102003865B1 (ko) * 2017-04-20 2019-07-26 한국생산기술연구원 액체금속을 이용한 메탄 열분해 및 고순도 수소, 일산화탄소 생산 장치 및 방법
US20180319660A1 (en) * 2017-05-04 2018-11-08 Honeywell International Inc. Integrated system for oxygen recovery for deep space mission

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