Process for performing endothermic production processes and plant for performing the process

Abstract

The present invention relates to a process for performing endothermic production processes, in particular high-temperature production processes, where minerals are thermally converted with release of carbon dioxide (CO2), where the thermal energy supplied to the production process is produced by combustion of a fuel, wherein the fuel employed contains or consists of DME (dimethyl ether).

Description

[0001] DESCRIPTION

[0002] Process for carrying out endothermic production processes and plant for carrying out the process

[0003] The present invention relates to a method for carrying out endothermic production processes, in particular high-temperature production processes in which minerals are thermally converted with the release of carbon dioxide (CO2), in which the thermal energy supplied to the production process is generated by the combustion of a fuel. Furthermore, the invention relates to a plant for carrying out such an endothermic production process, comprising a combustion chamber / burner in which the thermal energy required for the production process is generated by the combustion of a fuel.

[0004] A variety of products, such as glass and cement, are produced by the thermal conversion of minerals. In glass production, various minerals are mixed and melted. These include, in particular, soda (Na2CO3) and potash (K2CO3). When these substances are heated, carbon dioxide (CO2) is formed as a byproduct of glass production.

[0005] During cement production, calcium carbonate (CaCO2) is converted into calcium oxide (CaO) when the clinker is burned, and gaseous carbon dioxide (CO2) is also released.

[0006] The endothermic production processes described above are typically fired using natural gas or other fossil fuels. The carbon dioxide produced or released in the endothermic production process is removed along with the flue gases generated during the combustion process.

[0007] Since the carbon dioxide released during the production process does not come from a combustion process but from the essential input materials, CO2 emissions are currently classified as unavoidable. In the production of flat gas, approximately one-third of CO2 emissions are attributable to the input materials. The same process also occurs in cold plants.

[0008] In order to reduce CO2 emissions from these production processes, both the direct use of electrical energy from renewable energy sources such as photovoltaics or wind power and the use of non-fossil fuels such as hydrogen (H2) and ammonia (NH3) are being tested.

[0009] The capture of CO2 from flue gases and subsequent storage in rock layers (Carbon Capture and Storage CCS) is also being discussed. However, this process is very complex. Furthermore, CO2 storage carries long-term risks, is not socially acceptable in Germany, and is only being implemented with delays, as it currently takes a very long time for appropriate reservoirs to be qualified and approved. Furthermore, this technology can only reduce emissions by approximately 90%.

[0010] Since the sustainable production of hydrogen (H2) or ammonia (NH3) is highly energy-intensive and therefore difficult to implement in Central and Northern Europe, imports are necessary to supply local industrial plants. Because hydrogen is difficult to transport over long distances as a gas, it must be liquefied (LH2). Alternatively, the hydrogen can be converted through chemical reactions into liquid organic hydrogen carriers (LOHC) or into liquid or easily liquefiable hydrogen carriers such as ammonia (NH3) for transport.

[0011] There is currently no developed infrastructure for liquid hydrogen. Furthermore, liquefaction is very energy-intensive. Currently, relatively small liquefiers with a capacity of 5–30 tpd of H2 are still being built. These require up to 12 kWh / kg of hydrogen for liquefaction. Therefore, the transport of hydrogen via bulk chemicals such as ammonia (NH3) is preferred, as the transport infrastructure for these is available.

[0012] However, the direct use of ammonia as fuel gas requires a complex NO XRemoval and burner design are important due to the poor fuel gas properties of ammonia. Unlike power plants, however, glass and cement plants do not have gas processing systems such as DeNox or FGD. For this reason, in many concepts, the ammonia is first decomposed into nitrogen (N2) and hydrogen (H2) or into forming gas (a stoichiometric mixture of N2 and H2 in a ratio of 1:3) by an NH3 cracker and then used in the furnace. However, this leads to energy losses on the one hand and high capital costs on the other.

[0013] US 2019 / 0359894 A1 and WO 2017 / 088981 A1 also disclose the production of synthetic fuels from hydrogen on the one hand and carbon dioxide or carbon monoxide on the other. However, these processes are similarly complex to the process described above.

[0014] The object of the present invention is therefore to design a method for carrying out endothermic production processes of the type mentioned above in such a way that CO2 emissions can be reduced or avoided. Furthermore, a plant for carrying out the method is to be specified. This object is achieved according to the invention in a method of the type mentioned above in that a fuel is used which contains or consists mainly of DME (dimethyl ether). Accordingly, the plant for carrying out the method is characterized in that the burner is designed to burn a fuel which contains or consists mainly of DME (dimethyl ether).

[0015] According to one embodiment of the invention, a fuel is used that contains more than 50 mol%, in particular more than 60 mol%, of DME. According to a preferred embodiment, a fuel is used that contains at least 75 mol%, in particular at least 85 mol%, and in particular more than 90 mol% of DME. In one operating mode of the process, in particular, a gaseous fuel is burned that, apart from impurities, contains exclusively DME.

[0016] Accordingly, the plant for carrying out the process is characterized in that the burner—also called a furnace burner—is designed to burn a gaseous fuel containing more than 50 mol%, in particular more than 60 mol%, of DME. Preferably, the burner is designed to burn a gaseous fuel containing more than 70 mol%, in particular more than 85 mol%, and preferably more than 95 mol%, of DME, wherein the burner should be designed to burn a gaseous fuel containing, apart from impurities, exclusively DME.

[0017] The invention is therefore based on the idea of ​​using dimethyl ether as a fuel for firing the production process. Dimethyl ether is a fuel that can be produced from CO2 and sustainably produced hydrogen. In other words, the combustion process only releases CO2 that was previously extracted from the environment to produce dimethyl ether. This makes the combustion process and the DME production process combined CO2-neutral.

[0018] According to one embodiment of the invention, it can further be provided that carbon dioxide (CO2) is separated from the flue gas / gas mixture produced during the combustion of the fuel and / or during the production process. For this purpose, a corresponding CO2 separation device is provided downstream of the burner. The carbon dioxide (CO2) is expediently separated from the flue gas produced during the combustion of the fuel and the flue gas produced during the production process in a joint CO2 separation system.

[0019] CO2 capture can be carried out, for example, using DME as a scrubbing agent. In this case, the flue gas / gas mixture is conveniently dried before CO2 capture. It is also possible to separate some of the water contained in the flue gas / gas mixture through condensation. Condensation of the water takes place at temperatures as low as possible above freezing. After scrubbing with DME, the flue gas can be further scrubbed with water to prevent DME losses.

[0020] Alternatively, the CO2 removal can be carried out by chemical scrubbing, in particular by amine scrubbing in one or two stages and / or by physical scrubbing, in particular based on methanol and / or by a membrane process and / or by an adsorption process.

[0021] Here, too, it is possible to at least partially liquefy the carbon dioxide (CO2) separated from the flue gas. For CO2 liquefaction, waste heat from DME evaporation is conveniently used. To achieve this, the carbon dioxide (CO2) is liquefied at a higher pressure than the DME is evaporated. Since DME can be evaporated at a lower pressure, the carbon dioxide (CO2) only needs to be compressed above the critical pressure before liquefaction. Overall, the process is energy-efficient.

[0022] The carbon dioxide (CO2) separated from the flue gas / gas mixture is preferably fed into a DME production process to create a closed cycle. Since the DME production process is very energy-intensive, it will usually take place spatially separate from the endothermic production process. In this case, the carbon dioxide (CO2) is transported to the DME production site using transport vehicles. Tankers can be used as a means of transport, with tankers being preferred for transporting DME from the DME production site to the endothermic production process site. This design is based on the consideration that the physical properties of DME and CO2 are very similar, so that CO2 and DME can be transported or stored in the same transport vessel using the same tanks.The tanks can either be equipped with a membrane so that DME and CO2 do not mix, or additional stationary tanks can be installed to prevent mixing of DME and CO2.

[0023] Overall, the invention creates a closed CO2 cycle in which the CO2 released during DM E combustion is captured and fed back into DME production as a carbon source. This eliminates CO2 storage, and the environment is not burdened with CO2 emissions due to the combustion itself. The process according to the invention even makes it possible to avoid some of the CO2 emissions released during the conversion of minerals, which are therefore considered unavoidable. To achieve this, it is merely necessary to separate more CO2 from the flue gas / gas mixture than is required for the production of the DME used. In this way, CO2 losses elsewhere in the supply chain can be compensated.

[0024] According to the invention, DME is used as the fuel. At times when no DME or insufficient DME is available, the process can also be carried out using other fuels. Thus, in at least one operating mode of the process, a fuel can be used which mainly contains DME and additionally other fuels, in particular hydrogen (H2) and / or methane (CH4). In a further operating mode of the process, a fuel which contains pure hydrogen (H2) and / or methane (CH4) without DME can be used for a limited time. Finally, an operating mode is also conceivable in which the thermal energy is generated at least partially via electrical energy.

[0025] Since dimethyl ether is usually transported in liquid form, one embodiment of the process according to the invention provides for the DME (dimethyl ether) to be supplied in liquid form and vaporized before combustion. For this purpose, a corresponding vaporization device is provided upstream of the burner. The gaseous DME is preferably burned without further conversion into a hydrogen carrier other than DME, in particular without a reforming step following vaporization. In this embodiment, the burner is structurally connected directly to the vaporization device, i.e. without the interposition of a device for converting the gaseous DME into a hydrogen carrier other than DME, such as a reforming device, in order to feed the gaseous DME directly to the burner.

[0026] In a further development of the method according to the invention, it is provided that pure oxygen (O2) is supplied to the production process and / or combustion for O2 enrichment, wherein, in particular, the oxygen (O2) is generated by means of electrolysis from water and / or by cryogenic air separation and / or by a high-temperature membrane process and / or wherein, in particular, carbon dioxide (CO2) produced during combustion is separated from the flue gas generated during the production process by means of condensation. In this embodiment, the combustion air is enriched with oxygen (O2) (oxyfuel process) to achieve better efficiency. The oxygen (O2) is generated by means of electrolysis from water and / or by cryogenic air separation and / or by a high-temperature process.As a rule, the maximum flame temperature must be observed when oxygenating the combustion air, so that oxygen enrichment (without recycle) is limited. In this case, CO2 separation takes place as described above, but is more efficient due to the higher CO2 partial pressure. According to the invention, unconverted oxygen (O2) is separated from the flue gas produced during fuel combustion and / or the production process, and the oxygen (O2) is returned to the production process and / or combustion. A certain proportion of CO2, which has been separated from the flue gas, can also be added to the oxygen (O2) to adjust the flame temperature.

[0027] To further increase efficiency, it is possible to use waste heat from the flue gas generated during combustion and / or the production process to preheat combustion air and / or to evaporate DME.

[0028] As already described, soda (Na2COs) and / or potash (K2CO3) and / or calcium carbonate (CaCOs) can be thermally converted in the endothermic production process.

[0029] For further embodiments of the invention, reference is made to the claims and the following description with reference to the accompanying drawings. The drawing shows:

[0030] Figure 1 is a diagram in which the method according to the invention for carrying out endothermic production processes is schematically shown,

[0031] Figure 2 is a circuit diagram showing an example of CO2 separation from flue gas produced by the process according to the invention, and

[0032] Figure 3 is a circuit diagram schematically showing the treatment of the flue gas produced in the method according to the invention for carrying out endothermic production processes when using DME-based oxyfuel.

[0033] Figure 1 schematically shows the method according to the invention for carrying out endothermic production processes with DME firing and CO2 separation (carbon capture CC). The method is carried out in a plant which has as main components an evaporation device 1 for evaporating liquid dimethyl ether (DME), a combustion chamber or burner 2 in which the endothermic production process is carried out, the burner 2 being fired by the combustion of gaseous DME, and a CO2 separation device 3 downstream of the burner 2, in which carbon dioxide (CO2) is separated from the flue gas produced during the production process and combustion.

[0034] During operation, liquid DME is fed to the evaporation device 1, as indicated by arrow A in Figure 1, and the DME is converted into a gaseous state in the evaporation device 1. The energy required for this can be provided at least partially by the waste heat from the flue gas generated during combustion in the production process, as will be described below.

[0035] The gaseous fuel is fed directly from the evaporation device 1 to the burner 2, where it is combusted with combustion air to generate the thermal energy required for the endothermic production process. The combustion air required for combustion can optionally be enriched with oxygen (O2) (oxyfuel process) to improve combustion efficiency (see arrow B in Figure 1). As a rule, the maximum flame temperature must be observed when oxygenating the combustion air. To adjust the flame temperature, a certain amount of carbon dioxide (CO2) can be added to the oxygen (O2), which is then recycled from the CO2 separation device 3 to the production process.

[0036] Oxygen (O2) is generated from water by electrolysis and / or by cryogenic air separation and / or by a high-temperature membrane process. By enriching the combustion air with oxygen (O2), oxygen (O2) not converted during combustion can also be separated from the flue gas and recycled to enrich the combustion air with oxygen. The recycling of carbon dioxide (CO2) and oxygen (O2) will be discussed below.

[0037] Burner 2 is also supplied with carbon-containing feedstocks / minerals, which represent the input materials of the production process (see arrow C in Figure 1).

[0038] In glass production, for example, various minerals are mixed and melted. These include, in particular, soda (Na2CO3) and potash (K2CO3), which, when heated, produce carbon dioxide (CO2) as a byproduct of glass production.

[0039] Likewise, the production process can be the burning of clinker to produce cement, in which calcium carbonate (CaCOs) is converted into calcium dioxide (CaO) with the release of carbon dioxide (CO2).

[0040] The burner 2 is designed according to the invention to burn gaseous DME.

[0041] Preferably, the burner 2 is further configured to also combust other fuels, in particular hydrogen (H2) and / or methane (CH4). In this case, it is possible to fire the furnace burner 2 with a mixture of gaseous DME, hydrogen, and / or methane. At times when no DME is available, a fuel containing pure hydrogen (H2) and / or methane (CH4) without DME can then be used for a limited time in an operating mode of the process according to the invention. An operating mode is also conceivable in which the thermal energy is generated at least partially via electrical energy. The CO2 separation in the CO2 separation device 3 can be carried out in the usual way by chemical scrubbing, in particular by amine scrubbing in one or two stages, and / or by physical scrubbing, in particular based on methanol, and / or by a membrane process and / or by an adsorption process.

[0042] From the CO2 separation device 3, the CO2-poor flue gas is released into the environment, if necessary after further treatment stages, as indicated by the arrow E in Figure 1, and the separated CO2 is transported back to the site of DME production, if necessary after liquefaction, to serve there as a carbon source for DME production (see arrow F in Figure 1).

[0043] Since the physical properties of DME and CO2 are very similar, the CO2 and DME can be transported and stored in the same transport vessel using the same tanks. The tanks can be equipped with a membrane to prevent DME and CO2 from mixing. Alternatively, at least one additional stationary tank can be installed on the transport vessel to prevent DME and CO2 from mixing.

[0044] Figure 2 illustrates in more detail a process for separating CO2 from the flue gas in the CO2 separation device 3. The flue gas D coming from the burner 2 is first cooled in a heat exchanger 4 and then fed via a flue gas blower 5 to another heat exchanger 6, in which heat is extracted from the flue gas D and fed to the liquid DME for evaporation. The heat exchanger 6 thus also forms part of the evaporation device 1. The flue gas, now cooled to approximately 5°C, is fed to a drying unit 7, in which condensate condensed from the flue gas is removed (see arrow G).

[0045] From the drying unit 7, the flue gas is fed to a first scrubbing column 8, see arrow H in Figure 2. In the scrubbing column 8, the actual CO2 removal from the flue gas takes place, for example, using DME as a scrubbing agent. Additionally, a cleaning process with water (H2O) is performed. For this purpose, DME is fed to one point of the scrubbing column 8, water (H2O) is fed to another point, and a mixture of DME and water is fed to another point. The scrubbing process is known per se and will therefore not be described in detail.

[0046] The purified flue gas is discharged from scrubbing column 8 at point E1, and water and a mixture of DME and CO2 are discharged from scrubbing column 8 at point I. This stream is first compressed or conveyed in a pump 9 and fed into a separation column 10. On its way from pump 9 to separation column 10, the stream passes through a heat exchanger 11, where it is cooled. The heat is used to heat a mixture of DME and water, which is fed to the first scrubbing column 8.

[0047] In the separation column 10, CO2 is obtained at the top and a mixture of DME and H2O is obtained in the bottom.

[0048] The mixture of DME and H2O is fed from the separation column 10 via a line 12 to a heat exchanger 13, where it is cooled, and then to another separation column 14, where the DME is purified from the water. The DME / H2O mixture is discharged via a line 15. A portion of the mixture is evaporated in a reboiler 16 and fed back into the separation column 14 via a separation device 18. The DME is recycled to the first scrubbing column 8, and the water is released to the environment. A portion of the water is recycled via line 19 to the first scrubbing column 8 to prevent DME emissions in the flue gas stream E1. Inert gases can be released to the environment via the top (see arrow E3).

[0049] A mixture of DME and H2O is partially taken from the first wash column 8 (see arrow K) and fed directly into the separation column 10 or into the separation column 14.

[0050] Figure 3 shows the treatment of flue gas when the DME fuel is enriched with oxygen during combustion, i.e., an oxyfuel is burned. In this case, the flue gas D coming from the furnace burner 2 is rich in carbon dioxide (CO2), water (H2O), and oxygen (O2). The flue gas stream is cooled in a heat exchanger 20 and fed to a first drying unit 21. In this drying unit 21, liquid condensate is separated from the flue gas and removed (see arrow M). The thus pre-dried flue gas is fed via a line 22 to a compressor

[0051] 23 and compressed there, and then in a heat exchanger

[0052] 24 and fed to a second drying unit 25, in which liquid condensate is again separated from the flue gas (see arrow N).

[0053] The remaining flue gas is partially recycled via line 26 to be mixed with the oxygen used to enrich the combustion air.

[0054] The remaining flue gas (line 27) is further compressed in a compressor 28, cooled in a heat exchanger 29, and then fed to a third drying unit 30, where liquid condensate is separated from the flue gas (see arrow O). The flue gas exiting the third drying unit 30 is fed to a fourth drying unit 32 via a line 31, where water is separated from the flue gas (see arrow P). The flue gas exiting the fourth drying unit 30 is only practically water-free and is cooled again in a heat exchanger 33. In a CO2 liquefaction unit 34, CO2 is condensed at approximately -50°C, and the CO2 condensate is removed for further use (see arrow Q).

[0055] The flue gas stream leaving the fifth drying unit 34 is rich in oxygen (O2). Part of it is recycled to the furnace burner 2 for O2 enrichment (line 35) and the rest is purified to remove inert components before being released into the environment (arrow E4).

[0056] List of reference symbols

[0057] 1 evaporation device

[0058] 2 burners

[0059] 3 CO2 separation device

[0060] 4 heat exchangers

[0061] 5 flue gas blowers

[0062] 6 heat exchangers

[0063] 7 Drying unit

[0064] 8 first wash column

[0065] 9 Pump

[0066] 10 Separation column

[0067] 11 heat exchangers

[0068] 12 Line

[0069] 13 heat exchangers

[0070] 14 Separation column

[0071] 15 Line

[0072] 16 reboilers

[0073] 17 heat exchangers

[0074] 18 Separator

[0075] 19 Management

[0076] 20 heat exchangers

[0077] 21 first drying unit

[0078] 22 Line

[0079] 23 compressors

[0080] 24 heat exchangers

[0081] 25 second drying unit

[0082] 26 Line

[0083] 27 Line

[0084] 28 Compressor 29 Heat exchanger

[0085] 30 third drying unit

[0086] 31 Line

[0087] 32 fourth drying unit 33 heat exchanger

[0088] 34 CO2 liquefaction

[0089] 35 Line

Claims

CLAIMS 1. A process for carrying out endothermic production processes, in particular high-temperature production processes, in which minerals are thermally converted with the release of carbon dioxide (CO2), in which the thermal energy supplied to the production process is generated by combustion of a fuel, characterized in that a fuel is burned which contains or consists of DME (dimethyl ether).

2. Process according to claim 1, characterized in that a fuel is burned which contains more than 50 mol%, in particular more than 60 mol% DME.

3. A process according to claim 1, characterized in that a fuel is burned which contains at least 75 mol%, in particular at least 85 mol% and in particular more than 90 mol% DME, wherein, in particular, at least in one operating mode of the process a fuel is used which, apart from impurities, contains exclusively DME.

4. Method according to one of the preceding claims, characterized in that at least in one operating mode of the method, a fuel is used which mainly comprises DME and additionally other fuels, in particular hydrogen (H2) and / or methane (CH4).

5. Process according to one of the preceding claims, characterized in that the DME (dimethyl ether) is supplied in liquid form and evaporated before combustion in order to bring it into a gaseous state, wherein, in particular, the gaseous DME is used without further reaction. into a hydrogen carrier other than DME, in particular without a reforming step following the evaporation.

6. Method according to one of the preceding claims, characterized in that pure oxygen (O2) is supplied to the production process and / or the combustion for O2 enrichment, wherein, in particular, the oxygen (O2) is produced by means of electrolysis from water and / or by cryogenic air separation and / or by a high-temperature membrane process and / or wherein, in particular, carbon dioxide (CO2) produced during the combustion and / or the production process is separated by means of condensation from the flue gas produced during the production process and / or the combustion.

7. Method according to one of the preceding claims, characterized in that carbon dioxide (CO2) is separated from the flue gas / gas mixture produced during the combustion of the fuel and / or during the production process, and / or that carbon dioxide (CO2) is separated from the flue gas / gas mixture produced during the combustion of the fuel and the flue gas / gas mixture produced during the production process in a common CO2 separation.

8. A process according to claim 7, characterized in that the carbon dioxide (CO2) separated from the flue gas / gas mixture is at least partially liquefied.

9. Process according to claim 8 and claim 5, characterized in that waste heat from the CO2 liquefaction is used for DME evaporation.

10. Process according to one of claims 7 to 9, characterized in that the CO2 separation is carried out using DME as a scrubbing agent, wherein in particular the flue gas is dried before the CO2 separation and / or a part of the water contained in the flue gas is separated by condensation.

11. Process according to claim 10, characterized in that the flue gas is additionally washed with water after washing with DME.

12. Process according to one of claims 7 to 11, characterized in that the CO2 separation is carried out by chemical washing, in particular by amine washing in one or two stages, and / or by physical washing, in particular based on methanol, and / or by a membrane process and / or in the adsorption process.

13. A process according to any one of claims 7 to 12, characterized in that carbon dioxide (CO2) separated from the flue gas / gas mixture is fed to a process for producing DME.

14. The process according to claim 13, characterized in that the DME produced is returned to the process.

15. The method according to claim 13 or 14, characterized in that the process for producing DME takes place spatially separated from the endothermic production process and the CO2 is transported to the place of production of DME by means of transport.

16. Method according to claim 15, characterized in that tankers are used as the means of transport, in particular the same tankers are used as those used to transport DME.

17. Method according to one of the preceding claims, characterized in that oxygen (O2) is separated from the flue gas / gas mixture produced during the combustion of the fuel and / or during the production process and the oxygen (O2) is returned to the production process and / or the combustion, wherein, in particular, carbon dioxide (CO2), which has also been separated from the flue gas, is added to the oxygen (O2).

18. Method according to one of the preceding claims, characterized in that waste heat from the flue gas / gas mixture which arises during the combustion and / or the production process is used to preheat combustion air and / or to evaporate DME.

19. Process according to one of the preceding claims, characterized in that in the endothermic production process soda (Na2CO3) and / or potash (K2CO3) and / or calcium carbonate (CaCO3) are thermally converted.

20. Plant for carrying out endothermic production processes in a method according to one of the preceding claims, with a combustion chamber / burner (2) in which the thermal energy required for the production process is generated by combustion of a fuel, characterized in that the burner (2) is designed to burn a fuel containing or consisting of DME (dimethyl ether).

21. Plant for carrying out endothermic production processes according to claim 20, characterized in that the burner (2) is designed to burn a fuel which contains more than 50 mol%, in particular more than 60 mol% DME.

22. Plant for carrying out endothermic production processes according to claim 21, characterized in that the burner (2) is designed to burn a gaseous fuel which contains more than 70 mol%, in particular more than 85 mol% and preferably more than 95 mol% DME, and / or that the burner (2) is designed to burn other fuels in addition to DME, in particular hydrogen and / or methane.

23. Plant for carrying out endothermic production processes according to one of claims 20 to 22, characterized in that an evaporation device (1) is provided upstream of the burner (2) in order to evaporate liquid DME and thus bring it into a gaseous state, wherein, in particular, the evaporation device (1) is connected to the burner (2) directly, that is to say without the interposition of a device, in particular a reforming device, for converting the gaseous DM Es into a hydrogen carrier other than DME, in order to feed the gaseous DME directly to the burner (2).

24. Plant for carrying out endothermic production processes according to one of claims 20 to 23, characterized in that a CO2 separation device (3) is provided downstream of the burner (2) in order to separate carbon dioxide (CO2) from the flue gas / gas mixture produced during the production process and / or combustion.

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