Device for separately collecting at least one of solid-state carbon and carbide from co2 gas, and method therefor

Abstract

To provide a device capable of separately collecting at least one of solid-state carbon and carbide from CO2 gas at low running cost, and to provide a method therefor.SOLUTION: A liquid metal storage container 1 stores liquid tin (Sn, a melting point of 232°C), and a CO2 gas is blown through a CO2 gas supply pipe 2. There is provided a product material discharge pipe 3 for separately collecting and discharging a product material at an upper portion of the liquid metal storage container 1. The liquid tin preheated with a liquid tin (Sn) replenishment pipe 5 made of stainless steel is replenished when liquid Sn inside the liquid metal storage container 1 is reduced. It is carried out by the liquid Sn (the melting point of 232°C) to separately collect solid-state carbon from the CO2 gas. That is, the liquid Sn and the CO2 gas are reacted as follows. Sn + CO2 → SnO2 + C The Sn itself is also oxidized to discharge tin oxide (SnO2) as the product material together with the solid-state carbon C from the product material discharge pipe 3, while separately collecting the solid-state carbon.SELECTED DRAWING: Figure 1

Description

[Technical field]

[0001] The present invention relates to an apparatus and method for separating and recovering solid carbon or carbides from CO2 gas using liquid tin (Sn) or liquid tin alloys (SnAl, SnAlSi(Ti)). [Background technology]

[0002] In recent years, greenhouse gases (GHS) in the atmosphere (such as CO2 gas, CH4 gas, N2O gas, and alternative fluorocarbon gases) have made it difficult for heat to escape from the earth, causing global warming, which is causing the earth's temperature to rise.

[0003] Greenhouse gas emissions are calculated by multiplying the amount of each gas's emissions by the global warming potential (GWP), which indicates how many times larger a greenhouse gas is than CO2 gas, and as a result, CO2 gas accounts for 90.8% of greenhouse gas GHS. Therefore, in order to reduce greenhouse gas GHS, technology is needed to separate and capture emitted CO2 gas, fix it, or reuse it.

[0004] In the conventional CO2 gas separation and capture method, exhaust gas from a thermal power plant or the like is brought into contact with an amine solution, and high-concentration CO2 gas of about 15 vol% is adsorbed and absorbed by the amine solution, and the remaining exhaust gas is returned to the atmosphere.The amine solution is then heated to about 120°C to separate and capture about 100% of the ultra-high-concentration CO2 gas, and the amine solution is regenerated.

[0005] The method for storing the above-mentioned separated and captured CO2 gas is the reservoir storage method, in which the separated and captured CO2 gas is liquefied, transported by ship, and then injected and stored in a reservoir more than 800 meters underground on the seabed. Since many large-scale CO2 gas emission sources are located in coastal areas, storage below the seabed is suitable.

[0006] However, the above-mentioned reservoir storage method requires a barrier layer above the reservoir to prevent CO2 gas from leaking. In addition, it is necessary to prevent earthquakes or to ensure social acceptance of the health hazards that may occur if CO2 gas leaks. Furthermore, it is necessary to establish monitoring to detect CO2 gas leakage. Therefore, the reservoir storage method is inappropriate, and even if the separated and captured CO2 gas is fixed, the CO2 gas is not effectively utilized. Therefore, it is necessary to effectively utilize the separated and captured CO2 gas.

[0007] The first method for activating the separated and captured CO2 gas is a CO2 gas reforming method. That is, this is a CO2 gas reforming method in which CO2 gas and natural gas are reacted to synthesize synthetic gas (CO2+H2) as a chemical raw material, which is used to manufacture raw materials for internal combustion engines, plastics, fertilizers, etc. That is, first, synthetic gas (CO2+H2) is synthesized by a main reaction with CH4, a component of natural gas. CO2+CH4→2CO+2H2 Also, from CO CO+2H2→CH3OH This methanol is used as fuel for internal combustion engines, as a raw material for adhesives, paints, pesticides, etc. Furthermore, from H2 3H2+N2→2NH3 This ammonia is used as a raw material for fertilizers, synthetic fibers, etc.

[0008] However, in the above-mentioned CO2 gas reforming method, carbon precipitates at the low temperatures used to synthesize synthesis gas, causing blockage of the gas flow (coking). In addition, methanol synthesis requires high temperatures (approximately 800°C) for CO separation. Furthermore, ammonia synthesis requires a catalyst that does not deteriorate even with long-term use. For these reasons, the method has not yet been put to practical use.

[0009] In addition, there are special methods of the above-mentioned CO2 gas reforming method, such as the methanation method and the olefin synthesis method. CO2+4H2→CH4+2H2O Methane can be used as fuel for power generation and as a raw material for city gas. In addition, according to the olefin synthesis method, 2CO2+6H2→C2H4+4H2O Ethylene is synthesized by this process. Ethylene can be used as a raw material for plastics.

[0010] However, the methanation method and the olefin synthesis method require the consumption of hydrogen as a reducing agent and a catalyst that does not deteriorate even after long-term use. Moreover, the methanation method has not yet been put to practical use.

[0011] The second method of utilizing the CO2 gas separated and recovered above is the enhanced oil recovery method, in which CO2 gas is injected into the oil layer of an oil field to make it easier to recover oil. Since CO2 gas is easily mixed with oil, when CO2 gas mixes with oil, the viscosity of the oil decreases, making it easier to push out the oil.

[0012] The third method for utilizing the separated and captured CO2 gas described above is carbon recycled concrete, in which concrete is produced using calcium carbonate, which is produced by reacting CO2 gas with calcium, and blast furnace slag, etc., produced during steelmaking.

[0013] However, none of the above-mentioned CO2 gas separation and recovery methods, the first, second and third validation methods, separates and recovers solid carbon or charcoal for reuse.

[0014] Therefore, there is a need to separate and recover at least one of solid carbon and char from CO2 gas and immobilize it.

[0015] FIG. 9 shows a conventional device for separating and recovering solid carbon from CO2 gas, where (A) is a block diagram and (B) is a cross-sectional photograph of the product produced (see Non-Patent Document 1).

[0016] 9A, a liquid metal container 101 for containing liquid GaIn (Ga 75 vol%: In 25 vol%) (melting point 15°C) is heated at a relatively low temperature and CO2 gas is blown in. As a result, the liquid metal alloy GaIn and CO2 gas react at a low temperature as shown in the following formula. 4GaIn+3CO2→2Ga2O3+3C Therefore, the solid carbon is separated and collected, and Ga itself is also oxidized to produce gallium oxide (Ga2O3), which is discharged together with the solid carbon C as a product, as shown in FIG. 9B. In this case, Ga2O3 and C can be physically separated, for example, by centrifugation. Therefore, Ga2O3 can be reused as Ga in liquid GaIn. In addition, no reducing agent is required, and the process is easy to integrate into existing engineering processes and scale up. Note that the base material liquid Ga in the liquid metal container 101 is consumed by the above-mentioned reaction, so it must be replenished. [Prior art documents] [Patent documents]

[0017] [Non-Patent Document 1] K.Zuraigi et al., Direct conversion of CO2 to solid carbon by Ga-based liquid metals, Energy Environ sci., 2022,15,595. Summary of the Invention [Problem to be solved by the invention]

[0018] However, in the conventional device for separating and recovering solid carbon from CO2 gas shown in Figure 9, although solid carbon can be separated and recovered, there is an issue that the running costs of the device are high because both Ga and In in liquid GaIn are very expensive (Ga is especially expensive). [Means for solving the problem]

[0019] In order to solve the above-mentioned problems, the device for separating and recovering solid carbon or carbide from CO2 gas according to the present invention comprises a liquid metal container for containing liquid tin, a container heating unit for heating the liquid metal container, a CO2 gas supply pipe for supplying CO2 gas to the liquid metal container, a CO2 gas supply heating unit for heating the CO2 gas supply pipe, and a product discharge pipe provided at the top of the liquid metal container for discharging from the liquid metal container a product generated by the reaction between liquid tin (Sn) and CO2 gas.

[0020] In addition, a method for separating and recovering at least one of solid carbon and carbides from CO2 gas according to the present invention includes the steps of heating liquid Sn, blowing heated CO2 gas into the heated liquid Sn, and discharging a product produced by the reaction between the liquid Sn and the CO2 gas. Effect of the Invention

[0021] According to the present invention, at least one of solid carbon and carbide can be separated and recovered from CO2 gas, and the products can be physically separated and reused. Furthermore, since Sn is cheaper than Ga and In, the running cost can be reduced. [Brief description of the drawings]

[0022] [Figure 1] 1 is an overview diagram showing a first embodiment of an apparatus for separating and recovering at least one of solid carbon and char from CO2 gas according to the present invention. [Diagram 2] 1 is a schematic view showing a second embodiment of an apparatus for separating and recovering at least one of solid carbon and char from CO2 gas according to the present invention. FIG. [Diagram 3] FIG. 2 is a phase diagram of an Al—Sn alloy for explaining the melting point of the Al—Sn alloy. [Figure 4] FIG. 4 is a graph showing the Gibbs free energy per oxygen atom in the reaction formula for oxide formation in liquid SnAl. [Diagram 5]1 is a schematic view showing a third embodiment of an apparatus for separating and recovering at least one of solid carbon and char from CO2 gas according to the present invention. FIG. [Figure 6] FIG. 11 is an overview diagram showing a fourth embodiment of the device for separating and recovering at least one of solid carbon and char from CO2 gas according to the present invention. [Figure 7] FIG. 7 shows an experiment of the apparatus of FIGS. 2, 5 and 6. [Figure 8] 8 is a cross-sectional photograph of the product obtained in the experiment of FIG. 7. [Figure 9] This shows a conventional device for separating and recovering solid carbon from CO2 gas. (A) is an overview, and (B) is a cross-sectional photograph of the resulting product. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0023] FIG. 1 is a schematic view showing a first embodiment of an apparatus for separating and recovering at least one of solid carbon and char from CO2 gas according to the present invention.

[0024] In FIG. 1, a stainless steel liquid metal container 1 contains liquid tin (Sn, melting point 232°C) and is heated to 500-700K by a mantle heater 1a. A stainless steel CO2 gas supply pipe 2 is installed from the top to the bottom of the liquid metal container 1, and CO2 gas is blown in. As a result, CO2 bubbles are generated in the liquid tin. The CO2 gas supply pipe 2 may be installed from the side of the liquid metal container 1 toward the inside. The CO2 gas supply pipe 2 is preheated to 500-700K by a ribbon heater 2a. A product discharge pipe 3 is installed at the top of the liquid metal container 1 to separate, collect, and discharge the product.

[0025] The CO2 gas supply pipe 2 supplies CO2 gas via a flow rate adjustment unit 4. When the liquid Sn in the liquid metal container 1 becomes low, liquid Sn preheated by a ribbon heater 5a is replenished from a stainless steel liquid tin (Sn) refilling pipe 5. The flow rate adjustment unit 4 and the liquid tin refilling pipe 5 are controlled by a control unit 6 configured by a computer or the like. The control unit 6 controls the mantle heater 1a based on the temperature of a thermocouple (not shown) provided in the liquid Sn, and controls the ribbon heater 2a based on the temperature of a thermocouple (not shown) provided in the CO2 gas supply pipe 2.

[0026] Solid carbon can be separated and recovered from CO2 gas using liquid Sn (melting point 232°C). That is, liquid Sn reacts with CO2 gas as follows: Sn+CO2→SnO2+C Therefore, the solid carbon is separated and collected, and Sn itself is also oxidized to produce tin oxide (SnO2), which is discharged from the product discharge pipe 3 together with the solid carbon C. In this case, the tin oxide (SnO2) and the solid carbon C are physically separated, and therefore the tin oxide (SnO2) can be separated from the solid carbon C by centrifugation or the like and reused as liquid Sn. However, since the liquid tin in the liquid metal storage vessel 1 is lost as a product, it is replenished from time to time via the liquid tin replenishment pipe 5.

[0027] Thus, in the apparatus of FIG. 1, liquid Sn is heated, heated CO2 gas is blown into the heated liquid Sn, and the product produced by the reaction between the liquid Sn and CO2 gas is discharged. Liquid Sn is replenished as needed. The product is tin oxide and solid carbon. Therefore, compared to the conventional apparatus of FIG. 9, the melting point of Sn is higher than that of GaIn, but Sn is cheaper than Ga and In, so the running costs can be significantly reduced. For example, the market price of Sn is less than 1 / 200 of the market price of Ga and less than 1 / 20 of the market price of In.

[0028] FIG. 2 is a schematic view showing a second embodiment of the apparatus for separating and recovering at least one of solid carbon and char from CO2 gas according to the present invention.

[0029] 2, the liquid tin refill tube 5 is removed from the components in FIG. 1, and an additive supply tube 7 heated by a ribbon heater 7a is added. The additive supply tube 7 adds aluminum (Al) as an additive to the liquid metal container 1 to convert liquid Sn into liquid tin aluminum (SnAl). The control unit 6 controls the ribbon heater 7a based on the temperature of a thermocouple (not shown) provided in the additive supply tube 7.

[0030] As described below, liquid tin (Sn) is not discharged as a product, and therefore there is no need to replenish liquid Sn, which further reduces running costs.

[0031] FIG. 3 is a phase diagram of an Al—Sn alloy for explaining the melting point of the Al—Sn alloy.

[0032] As shown in Figure 3, the melting point of the eutectic point of 97.8 at% (99.95 vol%) Sn and 0.22 at% (0.05 vol%) Al is 228°C, whereas the melting point of 90 at% (97.54 vol%) Sn and 10 at% (2.46 vol%) Al is 380 to 390°C. Therefore, if Al is less than 10 at%, the melting point of tin-aluminum alloy (SnAl) can be considered to be relatively low at 230 to 400°C.

[0033] Figure 4 is a graph showing the Gibbs free energy per oxygen atom in the oxide formation reaction formula in liquid AlSn. The unit of the vertical axis in Figure 4 is the formation energy per oxygen atom, kJ / atom O.

[0034] As shown in FIG. 4, there are oxide production reaction formulas (1), (2), (3), (4), and (5). 1 / 2C+1 / 2O2→1 / 2CO2+1 / 2Δ f G°(CO2) (1) 1 / 2CO2+Sn→SnO+1 / 2C+Δ f G°(SnO) (2) 1 / 2CO2+1 / 2Sn→1 / 2SnO2+1 / 2C+1 / 2Δ fG°(SnO2) (3) 1 / 2CO2+2 / 3Al→1 / 3Al2O3+1 / 2C+1 / 3Δ f G° (Al2O3) (4) 1 / 4CO2+1 / 2Al→1 / 4Al4O4C+1 / 4C+1 / 4Δ f G° (Al4O4C) (5) At temperatures between 500 and 700 K, 1 / 2Δ f G°(CO2)>Δ f G°(SnO)>1 / 2Δ f G°(SnO2) >1 / 3Δ f G°(Al2O3)>1 / 4Δ f G°(Al4O4C) Therefore, reaction (5) is the most thermodynamically stable. Therefore, the products consist of aluminum oxide carbide (Al4O4C) and solid carbon (C). Aluminum oxycarbide and solid carbon can be physically separated, for example, by centrifugation.

[0035] The price of Al is cheaper than that of Ga, and the production volume of Al is about 160 times that of Ga. Aluminum oxycarbide (Al4O4C) has good thermal shock resistance, low thermal expansion coefficient, and oxidation resistance, and is expected to be used as a refractory material for molten metals such as steel. It is used to form a protective film (MgAl2O4) by adding it to MgO used in the walls of converter furnaces.

[0036] Thus, in the apparatus of FIG. 2, liquid aluminum tin is heated, heated CO2 gas is blown into the heated liquid aluminum tin, and the product produced by the reaction between the liquid aluminum tin and the CO2 gas is discharged. In this case, the base material liquid tin is not oxidized, so there is no need to replenish it. Only aluminum is added as appropriate. The products are aluminum oxycarbide and solid carbon. Therefore, compared to the conventional apparatus of FIG. 9, the melting point of SnAl is higher than that of GaIn, but since Sn and Al are cheaper than Ga and In, running costs can be significantly reduced. 。

[0037] FIG. 5 is a schematic view showing a third embodiment of the apparatus for separating and recovering at least one of solid carbon and char from CO2 gas according to the present invention.

[0038] In FIG. 5, an additive supply pipe 7 adds aluminum (Al) and silicon (Si) as additives into the liquid metal container 1 to convert liquid Sn into liquid tin aluminum silicon (SnAlSi).

[0039] The chemical reaction between the liquid SnAlSi and CO2 gas in Figure 5 is as follows: 2CO2+4Al+Si→Al4O4C+SiC(ΔG=-1332 kJ, at300K) 3CO2+4Al+3Si→2Al2O3+3SiC(ΔG=-1946 kJ, at300K) Therefore, alumina (Al2O3) is produced together with silicon carbide (SiC) rather than aluminum oxycarbide (Al4O4C). In this case, alumina (Al2O3) and silicon carbide (SiC) can be physically separated by centrifugation or the like.

[0040] In this way, in the apparatus of FIG. 5, liquid tin aluminum silicon is heated, heated CO2 gas is blown into the heated liquid tin aluminum silicon, and the product generated by the reaction between the liquid tin aluminum silicon and CO2 gas is discharged. In this case, the base material liquid Sn is not oxidized, so there is no need to replenish it. Only aluminum and silicon are added appropriately. The products are silicon carbide and alumina. Therefore, compared to the conventional apparatus of FIG. 9, the melting point of SnAlSi is higher than that of GaIn, but Sn, Al, and Si are cheaper than Ga and In, so the running costs can be significantly reduced.

[0041] The prices of Al and Si are cheaper than those of Ga, and their production volume is large. Alumina (Al2O3) with a purity of 99.5% is generally used. The higher the purity, the better the mechanical strength and corrosion resistance. Furthermore, it has electrical insulation properties, so it is used for semiconductor substrates, etc.; it has wear resistance, so it is used for wear parts of industrial furnace materials, artificial bones, bearings, etc.; it has high rigidity, so it is used for precision parts such as semiconductor and liquid crystal panel manufacturing equipment; and it has biocompatibility, so it is used for medical joint parts such as dental implants. On the other hand, silicon carbide (SiC) has high hardness (even at high temperatures), wear resistance, corrosion resistance, good sliding properties in liquids, and high breakdown electric field strength, so it is used for sliding parts (chemical pump bearings, shafts), crushers (classifiers), heat-resistant parts (burner nozzles), wear-resistant parts (blast nozzles), power semiconductors, etc. In particular, demand for it as a semiconductor is on the rise, and compared to silicon, it has 10 times the breakdown field strength, and the same breakdown voltage can be achieved with 1 / 10 the thickness, which helps to miniaturize electronic devices. In addition, it has three times the thermal conductivity of silicon, which makes it good at dissipating heat and allows for the miniaturization of cooling devices.

[0042] FIG. 6 is a schematic diagram showing a fourth embodiment of the apparatus for separating and recovering solid carbon or char from CO2 gas according to the present invention.

[0043] In FIG. 6, an additive supply pipe 7' adds aluminum (Al) and titanium (Ti) as additives into the liquid metal container 1 to convert liquid Sn into liquid tin aluminum titanium (SnAlTi).

[0044] The chemical reaction between the liquid SnAlTi and CO2 gas in Figure 6 is as follows: 2CO2+4Al+Ti→Al4O4C+TiC(ΔG=-1451 kJ, at300K) 3CO2+4Al+3Ti→2Al2O3+3TiC(ΔG-2304 kJ, at300K) Therefore, alumina (Al2O3) is produced together with titanium carbide (TiC) rather than aluminum oxycarbide (Al4O4C). In this case, alumina (Al2O3) and titanium carbide (TiC) can be physically separated by centrifugation or the like.

[0045] In this way, in the apparatus of FIG. 6, liquid tin aluminum titanium is heated, heated CO2 gas is blown into the heated liquid aluminum tin titanium, and the product produced by the reaction between the liquid aluminum tin titanium and the CO2 gas is discharged. In this case, the base material liquid Sn is not oxidized, so there is no need to replenish it. Only aluminum and titanium are added appropriately. The products are titanium carbide and alumina. Therefore, compared to the conventional apparatus of FIG. 9, the melting point of SnAlTi is higher than that of GaIn, but since Sn, Al, and Ti are cheaper than Ga and In, running costs can be significantly reduced. 。

[0046] The prices of Al and Ti are lower than that of Ga, and production volumes are large. The situation regarding alumina (Al2O3) is as described above. On the other hand, titanium carbide (TiC) has high hardness, high melting point, wear resistance, and electrical conductivity (almost independent of temperature), so it can be used for sputtering targets, cutting tools, arc welding electrodes, etc.

[0047] FIG. 7 is a diagram for explaining an experiment using the devices shown in FIGS.

[0048] First, referring to FIG. 7A, an alumina crucible 71 is prepared, and tin (Sn) and aluminum (Al) or aluminum (Al) and silicon (Si) or titanium (Ti) as an additive are placed in the alumina crucible 71 .

[0049] Next, referring to FIG. 7B, tin (Sn) and additives (Al, Si, Ti) are ground and heated to 300° C. or higher by a hot plate 72.

[0050] Next, referring to FIG. 7C, liquid Sn, liquid SnAl, liquid SnAlSi or liquid SnAlTi is obtained.

[0051] Next, referring to FIG. 7(D), liquid Sn, liquid SnAl, liquid SnAlSi, and liquid SnAlTi are filled into the liquid metal container 1, and the liquid metal container 1 is closed with a lid 1' to which a CO2 gas supply pipe 2 is fixed.

[0052] Finally, referring to FIG. 7(E), heated CO2 gas is blown in through the CO2 gas supply pipe 2.

[0053] Then, the liquid SnAl, SnAlSi, or SnAlTi is solidified. The product shown in the cross-sectional photograph of Figure 8 is formed on the solidified SnAl, SnAlSi, or SnAlTi obtained in this manner. In other words, the product is physically separated from the SnAlTi.

[0054] In the above-described embodiment, the mantle heater 1a and the ribbon heaters 5a, 7a, 7'a may be of other types, such as sheath heaters, hot plates, or heaters that utilize solar heat.

[0055] Furthermore, the present invention can be applied to any modifications within the obvious scope of the above-described embodiment. [Explanation of symbols]

[0056] 1, 101: Liquid metal container 1a: Mantle heater 2: CO2 gas supply pipe 2a: Ribbon heater 3:Product discharge pipe 4: Flow rate adjustment unit 5:Liquid tin refill tube 5a: Ribbon heater 6: Control unit 7, 7': Additive supply pipe 7a, 7'a: Ribbon heater

Claims

1. a liquid metal container for containing liquid tin; A container heating unit for heating the liquid metal container; The liquid metal container is filled with CO ２ CO for supplying gas ２ A gas supply pipe; The CO ２ CO for heating the gas supply pipe ２ A gas supply unit heating unit; A liquid metal container is provided at the top of the liquid metal container, and the liquid tin and the CO ２ a product discharge pipe for discharging a product generated by the reaction with the gas from the liquid metal storage vessel; CO ２ An apparatus for separating and recovering solid carbon from gas.

2. 2. The CO gas turbine according to claim 1, further comprising a liquid tin refill tube for refilling the liquid metal container with the liquid Sn. ２ An apparatus for separating and recovering solid carbon from gas.

3. 2. The CO composition of claim 1, wherein the product comprises tin oxide and solid carbon. ２ An apparatus for separating and recovering solid carbon from gas.

4. a liquid metal container for filling with liquid tin; A container heating unit for heating the liquid metal container; an additive supply tube for adding heated aluminum into the liquid metal container to convert the liquid tin into liquid tin-aluminum; The liquid metal container is filled with CO ２ CO for supplying gas ２ A gas supply pipe; The CO ２ CO for heating the gas supply pipe ２ A gas supply unit heating unit; A liquid metal container is provided at the top of the liquid metal container, and the liquid tin aluminum and the CO ２ a product discharge pipe for discharging a product generated by the reaction with the gas from the liquid metal storage vessel; CO ２ An apparatus for separating and recovering solid carbon and char from gas.

5. 5. The CO process of claim 4, wherein the product comprises aluminum oxycarbide and solid carbon. ２ An apparatus for separating and recovering solid carbon and char from gas.

6. a liquid metal container for filling with liquid tin; A container heating unit for heating the liquid metal container; an additive supply tube for adding heated aluminum and silicon into the liquid metal containment vessel to convert the liquid tin into liquid tin aluminum silicon; The liquid metal container is filled with CO ２ CO for supplying gas ２ A gas supply pipe; The CO ２ CO for heating the gas supply pipe ２ A gas supply unit heating unit; A liquid metal container is provided at the top of the liquid metal container, and the liquid tin aluminum silicon and the CO ２ a product discharge pipe for discharging a product generated by the reaction with the gas from the liquid metal storage vessel; CO ２ A device for separating and recovering carbon from gas.

7. 7. The CO process of claim 6, wherein the products consist of alumina and silicon carbide. ２ A device for separating and recovering carbon from gas.

8. a liquid metal container for filling with liquid tin; A container heating unit for heating the liquid metal container; an additive supply tube for adding heated aluminum and titanium into the liquid metal containment vessel to convert the liquid tin into liquid tin-aluminum-titanium; The liquid metal container is filled with CO ２ CO for supplying gas ２ A gas supply pipe; The CO ２ CO for heating the gas supply pipe ２ A gas supply unit heating unit; A liquid metal container is provided at the top of the liquid metal container, and the liquid aluminum tin titanium and the CO ２ a product discharge pipe for discharging a product generated by the reaction with the gas from the liquid metal storage vessel; CO ２ A device for separating and recovering carbon from gas.

9. 9. The CO process of claim 8, wherein the products consist of alumina and titanium carbide. ２ A device for separating and recovering carbon from gas.

10. heating the liquid tin; Heated CO in the heated liquid tin ２ injecting gas; The liquid tin and the CO ２ Discharging the product produced by the reaction with the gas. CO ２ A method for separating and recovering solid carbon from a gas.

11. 11. The method of claim 10, further comprising the step of replenishing the liquid Sn. ２ A method for separating and recovering solid carbon from a gas.

12. 11. The CO composition of claim 10, wherein the products consist of tin oxide and solid carbon. ２ A method for separating and recovering solid carbon from a gas.

13. heating the liquid tin; adding heated aluminum to the liquid Sn to convert it into liquid Sn-aluminum; Heated CO in the heated liquid tin aluminum ２ injecting gas; The liquid tin aluminum and the CO ２ Discharging the product produced by the reaction with the gas. CO ２ A method for separating and recovering solid carbon from a gas.

14. 14. The CO process of claim 13, wherein the products consist of aluminum oxycarbide and solid carbon. ２ A method for separating and recovering solid carbon from a gas.

15. Heating the liquid Sn; adding heated aluminum and silicon to the liquid Sn to convert it into liquid tin aluminum silicon; Heated CO in the heated liquid tin aluminum silicon ２ injecting gas; The liquid tin aluminum silicon and the CO ２ Discharging the product produced by the reaction with the gas. CO ２ A method for separating and recovering char from gas.

16. 16. The CO process of claim 15, wherein the products consist of alumina and silicon carbide. ２ A method for separating and recovering char from gas.

17. Heating the liquid Sn; adding heated aluminum and titanium to the liquid Sn to convert it into liquid aluminum tin; Heated CO in the heated liquid tin aluminum titanium ２ injecting gas; The liquid aluminum tin titanium and the CO ２ Discharging the product produced by the reaction with the gas. CO ２ A method for separating and recovering char from gas.

18. 18. The CO process of claim 17, wherein the products consist of alumina and titanium carbide. ２ A method for separating and recovering char from gas.

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