Solid carbon forming facility

Abstract

To provide a solid carbon forming facility which, even when the concentration of a gas component is varied, can adjust the concentrations of hydrogen and carbon monoxide in gas to a ratio suitable for solid carbon forming reaction.SOLUTION: A solid carbon forming facility includes: hydrogen supply means 2 to supply hydrogen; carbon monoxide production means 3A to produce carbon monoxide; a solid carbon forming reaction device 4 which has a catalyst for performing reduction and oxidation of the carbon monoxide and into which gas containing the hydrogen supplied from the hydrogen supply means 2 and the carbon monoxide produced in the carbon monoxide production means 3A is introduced, so that the action of the catalyst results in deposition of solid carbon; concentration ratio calculation means to calculate a concentration ratio (A / B) between the concentration (A%)of the hydrogen contained in the gas introduced into the solid carbon forming reaction device 4 and the concentration (B%) of the carbon monoxide contained in the gas; and control means 60 to control the hydrogen supply means 2 so that the concentration ratio (A / B) calculated by the concentration ratio calculation means is 0.05 to 2.0.SELECTED DRAWING: Figure 1

Description

[Technical Field]

[0001] The present invention relates to a solid carbonization facility for producing solid carbon. [Background technology]

[0002] Traditionally, most carbon materials have been made primarily from fossil fuels. In recent years, there has been a demand to reduce the amount of fossil fuel used in order to curb global warming and build a sustainable society, and there is a need to produce carbon materials without using fossil fuels.

[0003] Patent Document 1 discloses a technology in which a mixed gas of a carbon monoxide-containing gas and a hydrogen gas is used, the flow rate ratio of the carbon monoxide-containing gas to the hydrogen gas is set within a predetermined range, and solid carbon is precipitated by the action of an Fe-based metal catalyst on the mixed gas. [Prior art documents] [Patent documents]

[0004] [Patent Document 1] Japanese Patent Application Laid-Open No. 2007-55821 Summary of the Invention [Problem to be solved by the invention]

[0005] For example, when the solid carbonization technology disclosed in Patent Document 1 is applied to a gas containing carbon monoxide obtained by reducing carbon dioxide contained in combustion exhaust gas emitted from a waste incineration treatment facility or the like, the following problems are likely to occur.

[0006] That is, the concentration of gas components contained in the gas to be treated may fluctuate depending on the operating conditions of a waste incineration treatment facility, etc. Patent Document 1 does not specifically disclose a means for adjusting the flow rate ratio of carbon monoxide-containing gas to hydrogen gas in the gas to be treated to a predetermined range suitable for the solid carbonization reaction (carbon deposition reaction). For this reason, when the concentration of gas components contained in the gas to be treated fluctuates, the flow rate of hydrogen gas relative to the carbon monoxide-containing gas may become excessive or insufficient. If the flow rate of hydrogen gas becomes excessive, the amount of relatively expensive hydrogen gas used increases, resulting in an increase in production costs. On the other hand, if the flow rate of hydrogen gas is insufficient, the reaction rate of the solid carbonization reaction decreases.

[0007] The present invention has been made in consideration of the above-mentioned problems, and aims to provide a solid carbonization facility that can adjust the concentrations of hydrogen and carbon monoxide in gas to a ratio suitable for a solid carbonization reaction even if the concentrations of gas components fluctuate. [Means for solving the problem]

[0008] The solid carbonization equipment according to the present invention for solving the above problems has the following characteristic configuration: a hydrogen supply means for supplying hydrogen; carbon monoxide generating means for generating carbon monoxide; a solid carbonization reactor having a catalyst for reducing and oxidizing carbon monoxide, into which hydrogen supplied from the hydrogen supply means and a gas containing carbon monoxide generated by the carbon monoxide generation means are introduced and which deposits solid carbon by the action of the catalyst; a concentration ratio calculation means for calculating a concentration ratio (A / B) between a hydrogen concentration (A%) contained in the gas introduced into the solid carbonization reactor and a carbon monoxide concentration (B%) contained in the gas; a control means for controlling the hydrogen supply means so that the concentration ratio (A / B) calculated by the concentration ratio calculation means is 0.05 to 2.0; The purpose is to provide the following.

[0009] In the solid carbonization equipment of this configuration, the concentration ratio (A / B) between the concentration (A%) of hydrogen contained in the gas introduced into the solid carbonization reactor and the concentration (B%) of carbon monoxide contained in the gas is calculated by the concentration ratio calculation means. Then, the amount of hydrogen supplied by the hydrogen supply means is controlled by the control means so that the concentration ratio (A / B) calculated by the concentration ratio calculation means is 0.05 to 2.0. Therefore, even if the concentrations of gas components (hydrogen, carbon monoxide, etc.) contained in the gas introduced into the solid carbonization reactor fluctuate, the concentrations of hydrogen and carbon monoxide in the gas introduced into the solid carbonization reactor can be adjusted to a ratio (0.05 to 2.0) suitable for the solid carbonization reaction. This makes it possible to maintain a high solid carbonization reaction rate and produce solid carbon with high efficiency.

[0010] In the solid carbonization equipment according to the present invention, The carbon monoxide generating means is a carbon dioxide recovery device that recovers carbon dioxide contained in the combustion exhaust gas; a chemical looping reactor into which the hydrogen-containing gas supplied from the hydrogen supply means and the carbon dioxide-containing gas recovered by the carbon dioxide recovery unit are introduced and which generates carbon monoxide by utilizing a chemical looping reaction; It is preferred that the compound contains:

[0011] In the solid carbonization equipment having this configuration, a hydrogen-containing gas supplied from a hydrogen supply means and a carbon dioxide-containing gas recovered by a carbon dioxide recovery unit are introduced into a chemical looping reactor, and carbon monoxide is generated by utilizing a chemical looping reaction. Because the chemical looping reaction is not governed by equilibrium depending on temperature, carbon monoxide can be generated with a high conversion rate.

[0012] In the solid carbonization equipment according to the present invention, The carbon monoxide generating means is a carbon dioxide recovery device that recovers carbon dioxide contained in the combustion exhaust gas; a carbon dioxide electrolysis device that electrolyzes the carbon dioxide recovered by the carbon dioxide recovery device to generate carbon monoxide; It is preferred that the compound contains:

[0013] According to the solid carbonization equipment having this configuration, carbon dioxide captured by the carbon dioxide capture device is electrolyzed in the carbon dioxide electrolysis device to generate carbon monoxide. If the carbon dioxide electrolysis device is configured to electrolyze the captured carbon dioxide-containing gas using, for example, electricity generated by utilizing the heat of the combustion exhaust gas and / or electricity generated by utilizing renewable energy, there is no need to use electricity generated separately using fossil fuels, and carbon monoxide can be generated without newly emitting carbon dioxide, thereby contributing to carbon dioxide reduction.

[0014] In the solid carbonization equipment according to the present invention, The carbon monoxide generating means is a carbon dioxide recovery device that recovers carbon dioxide contained in the combustion exhaust gas; a reverse shift reactor into which a gas containing hydrogen supplied from the hydrogen supply means and carbon dioxide recovered by the carbon dioxide recovery unit is introduced, and which reduces the carbon dioxide in the gas by a reverse shift reaction to produce carbon monoxide; It is preferred that the compound contains:

[0015] In the solid carbonization equipment having this configuration, a gas containing hydrogen supplied from the hydrogen supply means and carbon dioxide recovered by the carbon dioxide recovery unit is introduced into the reverse shift reactor, and carbon monoxide is produced by reducing the carbon dioxide in the gas through the reverse shift reaction. For example, if the reverse shift reactor is configured to preheat the gas containing hydrogen supplied from the hydrogen supply means and carbon dioxide recovered by the carbon dioxide recovery unit when the gas is introduced, the thermal energy required for heating when reducing carbon dioxide to carbon monoxide can be reduced, and energy costs can be held down.

[0016] In the solid carbonization equipment according to the present invention, It is preferable that the system further comprises a heater that heats the gas flowing upstream of the solid carbonization reactor by heat exchange with the off-gas from the solid carbonization reactor.

[0017] In the solid carbonization equipment having this configuration, the gas flowing upstream of the solid carbonization reactor is introduced into the solid carbonization reactor, and when carbon monoxide in the gas is reduced to carbon, the gas is heated by heat exchange with the off-gas from the solid carbonization reactor. This makes it possible to reduce the thermal energy required for heating when reducing carbon monoxide to carbon in the solid carbonization reactor, thereby reducing energy costs.

[0018] In the solid carbonization equipment according to the present invention, It is preferable that the apparatus further comprises an off-gas introduction passage for introducing the off-gas from the solid carbonization reactor into the upstream side of the gas flow of the solid carbonization reactor.

[0019] In the solid carbonization equipment of this configuration, off-gas from the solid carbonization reactor is introduced into the upstream side of the gas flow of the solid carbonization reactor through the off-gas inlet passage. The off-gas contains carbon monoxide that was not converted into carbon in the solid carbonization reactor and carbon dioxide that is produced as a by-product. By recycling and reusing the off-gas containing carbon monoxide and carbon dioxide as a raw material for solid carbon, the yield of solid carbonization can be improved and the amount of carbon dioxide that is wasted and discharged without being solid carbonized can be reduced.

[0020] In the solid carbonization equipment according to the present invention, The concentration ratio calculation means a hydrogen concentration measuring means for measuring the concentration of hydrogen contained in the gas introduced into the solid carbonization reactor; a carbon monoxide concentration measuring means for measuring the concentration of carbon monoxide contained in the gas introduced into the solid carbonization reactor; Including, It is preferable to calculate the concentration ratio (A / B) based on the hydrogen concentration (A%) measured by the hydrogen concentration measuring means and the carbon monoxide concentration (B%) measured by the carbon monoxide concentration measuring means.

[0021] According to the solid carbonization equipment of this configuration, the concentration ratio (A / B) can be calculated by measuring the hydrogen concentration (A%) and the carbon monoxide concentration (B%) individually using the hydrogen concentration measuring means and the carbon monoxide concentration measuring means.

[0022] In the solid carbonization equipment according to the present invention, The hydrogen concentration measuring means a hydrogen concentration meter for detecting the concentration of hydrogen contained in the gas introduced into the solid carbonization reactor, It is preferable to measure the concentration of hydrogen contained in the gas introduced into the solid carbonization reactor based on the detection result of the hydrogen concentration meter.

[0023] According to the solid carbonization equipment of this configuration, the concentration of hydrogen contained in the gas introduced into the solid carbonization reactor can be directly measured, and therefore accurate data on the hydrogen concentration can be obtained.

[0024] In the solid carbonization equipment according to the present invention, The hydrogen concentration measuring means an upstream flow meter for detecting a flow rate of gas flowing upstream of the solid carbonization reactor; a downstream flow meter for detecting a flow rate of gas flowing downstream of the solid carbonization reactor; Including, It is preferable to measure the concentration of hydrogen contained in the gas introduced into the solid carbonization reactor based on the detection results of the upstream flow meter and the downstream flow meter.

[0025] The solid carbonization equipment of this configuration can indirectly measure the concentration of hydrogen contained in the gas introduced into the solid carbonization reactor, thereby making it possible to easily obtain data on the hydrogen concentration.

[0026] In the solid carbonization equipment according to the present invention, The concentration ratio calculation means an upstream flow meter for detecting a flow rate of gas flowing upstream of the solid carbonization reactor; a downstream flow meter for detecting a flow rate of gas flowing downstream of the solid carbonization reactor; Including, It is preferable to calculate the concentration ratio (A / B) based on the conversion rate of carbon monoxide to solid carbon obtained from the detection results of the upstream flow meter and the downstream flow meter.

[0027] With the solid carbonization equipment of this configuration, the concentration ratio (A / B) is calculated based on the conversion rate of carbon monoxide to solid carbon obtained from the detection results of the upstream flow meter and the downstream flow meter, so the concentration ratio (A / B) can be calculated without having to measure the hydrogen concentration (A%) and the carbon monoxide concentration (B%) separately. [Brief explanation of the drawings]

[0028] [Figure 1] FIG. 1 is a block diagram showing a schematic configuration of a solid carbonization facility according to a first embodiment of the present invention. [Figure 2] FIG. 2 is a graph showing the relationship between the conversion rate of carbon monoxide to solid carbon (solid carbonization reaction rate) and the concentration ratio of hydrogen and carbon monoxide. [Figure 3] FIG. 3 is a flowchart showing the procedure of the hydrogen supply amount control process in the first embodiment. [Figure 4] FIG. 4 is a block diagram showing a schematic configuration of a solid carbonization facility according to a second embodiment of the present invention. [Figure 5] FIG. 5 is a block diagram showing a schematic configuration of a solid carbonization facility according to a third embodiment of the present invention. [Figure 6] FIG. 6 is a block diagram showing a schematic configuration of a modified example (1) of the solid carbonization equipment according to the first embodiment of the present invention. [Figure 7] FIG. 7 is a block diagram showing a schematic configuration of a modified example (2) of the solid carbonization equipment according to the first embodiment of the present invention. [Figure 8]FIG. 8 is a flowchart showing the procedure of the hydrogen supply amount control process in the modified example (2) of the first embodiment. DETAILED DESCRIPTION OF THE INVENTION

[0029] The present invention will be described below with reference to the drawings. However, the present invention is not intended to be limited to the embodiments described below or the configurations shown in the drawings. In the following description, the exhaust gas supply line 23, the treated gas lines 41 to 45, the off-gas lines 37 and 38, and the hydrogen supply lines 12, 14, and 46 are gas pipelines formed of required pipes, ducts, etc.

[0030] First Embodiment <Overall structure> Fig. 1 is a block diagram showing a schematic configuration of a solid carbonization facility 1A according to a first embodiment of the present invention. The solid carbonization facility 1A shown in Fig. 1 is applied to a waste incineration treatment facility 10 equipped with a power generation facility, and includes a hydrogen supply means 2, a carbon monoxide generation means 3A, a solid carbonization reaction device 4, a gas treatment device 5, a controller 6, a hydrogen concentration measurement means 7, and a carbon monoxide concentration measurement means 8.

[0031] <Waste incineration treatment facility> The waste incineration treatment facility 10 is equipped with a combustion furnace for burning waste, a heat recovery device such as a boiler for recovering heat from the combustion exhaust gas generated by combustion in the combustion furnace, and an exhaust gas treatment device for removing dust and other contaminants contained in the combustion exhaust gas and detoxifying it. Examples of the combustion furnace include an incinerator for incinerating waste. The type of incinerator is not particularly limited, and examples include a stoker-type incinerator, a fluidized-bed incinerator, a kiln-type incinerator, and a gasification melting furnace.

[0032] <Means for supplying hydrogen> The hydrogen supply means 2 includes a water electrolysis device 11, a first hydrogen supply line 12, a hydrogen storage and supply device 13, and a second hydrogen supply line 14. The water electrolysis device 11 is connected to a power supply line 15 that supplies electric power from a power generation facility that generates electric power using the heat of combustion exhaust gas in the waste incineration treatment facility 10, and / or a power supply line 16 that supplies electric power from a power generation facility that generates electric power using renewable energy. The water electrolysis device 11 and the hydrogen storage and supply device 13 are connected via the first hydrogen supply line 12. The hydrogen storage and supply device 13 and a second reactor 32, which will be described later, are connected via the second hydrogen supply line 14.

[0033] The water electrolysis device 11 electrolyzes water using power supplied from a power generation facility via power supply lines 15 and 16 to produce hydrogen gas and oxygen gas. While detailed illustrations of the water electrolysis device 11 are omitted, examples of the water electrolysis device 11 include a water tank for storing water, a gas-impermeable and ion-permeable diaphragm disposed in the water tank so as to divide the water tank into a first chamber and a second chamber, an anode disposed in the first chamber, and a cathode disposed in the second chamber. When an electric current is applied between the anode and the cathode, oxygen gas is produced on the anode side and hydrogen gas is produced on the cathode side. The water electrolysis device 11 may use water supplied from a water supply source external to the waste incineration treatment facility 10. However, hydrogen gas and oxygen gas can be economically produced by using drain water discharged from a steam turbine or a cooling tower in the power generation facility. In the water electrolysis device 11, oxygen gas is also produced as a by-product of hydrogen gas produced by electrolysis of water. This by-product oxygen gas is temporarily stored and then put to effective use.

[0034] The hydrogen storage and supply device 13 stores hydrogen gas supplied from the water electrolysis device 11 via the first hydrogen supply line 12 and supplies the stored hydrogen gas to a hydrogen demander (a second reactor 32 described below) via a second hydrogen supply line 14. Although not shown in detail, the hydrogen storage and supply device 13 may include, for example, a device including a hydrogen gas tank, a booster, and a pressure reducing valve, in which the hydrogen gas supplied from the water electrolysis device 11 is stored in the hydrogen gas tank under pressure via the booster, and the compressed hydrogen gas stored in the hydrogen gas tank is reduced to a predetermined pressure by the pressure reducing valve before being supplied to a hydrogen demander. Another example of the hydrogen storage and supply device 13 is one in which a hydrogen storage alloy in a hydrogen storage alloy tank absorbs and retains hydrogen gas. The hydrogen storage and supply device 13 may take the form of, for example, a container in which the components (such as the hydrogen gas tank, the booster, and the pressure reducing valve) are housed and packaged for transport by vehicle or the like.

[0035] <Means for generating carbon monoxide> The carbon monoxide generating means 3A includes a carbon dioxide recovery device 21 and a chemical looping reactor 22.

[0036] <Carbon dioxide capture device> The carbon dioxide capture device 21 receives the combustion exhaust gas from the waste incineration treatment facility 10 after exhaust gas treatment via an exhaust gas supply line 23 and captures the carbon dioxide contained in the combustion exhaust gas. Examples of the carbon dioxide capture device 21 include devices using chemical absorption, membrane separation, physical absorption, solid absorption, and the like. The carbon dioxide capture device 21 using the chemical absorption method uses, for example, an amine absorption liquid and is configured to separate and capture only the carbon dioxide by chemically bonding (reacting) the carbon dioxide in the exhaust gas with the amine. The carbon dioxide capture device 21 using the membrane separation method uses a solid thin film with separation function and is configured to separate and capture carbon dioxide from the exhaust gas by utilizing its permeability selectivity. The carbon dioxide capture device 21 using the physical absorption method is configured to separate and capture carbon dioxide in the exhaust gas by dissolving it in a liquid. The carbon dioxide capture device 21 using the solid absorption method is configured to use zeolite, activated carbon, or the like as a physical adsorption adsorbent, or an inorganic porous material supporting alkali metals or amines as a chemical adsorption adsorbent, and separate and capture the carbon dioxide in the exhaust gas by adsorbing it onto the adsorbent.

[0037] <Chemical Looping Reactor> The chemical looping reactor 22 includes a first reactor 31, a second reactor 32, a catalyst forward path 33, and a catalyst return path 34. The first reactor 31 is connected to the carbon dioxide capture device 21 via a treated gas line 41. The second reactor 32 is connected to the hydrogen storage / supply device 13 via a second hydrogen supply line 14. The first reactor 31 and the second reactor 32 are connected via the catalyst forward path 33 and the catalyst return path 34 so that a catalyst (metal oxide catalyst) can be circulated.

[0038] In the chemical looping reactor 22, carbon dioxide from the carbon dioxide capture device 21 is supplied to the first reactor 31 via the treated gas line 41, where a reduction reaction occurs, thereby discharging (producing) carbon monoxide, and hydrogen from the hydrogen storage / supply device 13 is supplied to the second reactor 32 via the second hydrogen supply line 14, where an oxidation reaction occurs, thereby discharging water. In addition, in the chemical looping reactor 22, the catalyst oxidized in the first reactor 31 is sent to the second reactor 32 via the catalyst forward path 33, and the catalyst reduced in the second reactor 32 is sent to the first reactor 31 via the catalyst return path 34, thereby circulating the catalyst. This makes it possible to continue using the catalyst for a long period of time without deactivating it, even when reduction and oxidation are repeatedly performed in each of the reactors 31 and 32.

[0039] The chemical looping reactor 22 may be of a type in which a catalyst is fixed and the gas supplied to each reactor 31, 32 is switched. In this type of chemical looping reactor 22, each reactor 31, 32 is filled with a catalyst, and lines for supplying carbon dioxide and hydrogen are connected to each reactor 31, 32, respectively. Carbon dioxide is supplied to either the first reactor 31 or the second reactor 32, and a reduction reaction occurs in that reactor, thereby discharging (producing) carbon monoxide. Meanwhile, hydrogen is supplied to the other reactor of the first reactor 31 or the second reactor 32, and an oxidation reaction occurs in that reactor, thereby discharging water. In this case, the reactor to which carbon dioxide is supplied and the reactor to which hydrogen is supplied are appropriately switched over time in the first reactor 31 and the second reactor 32. This allows the catalyst to be used for a long period of time without being deactivated, even when oxidation and reduction of the catalyst are repeatedly performed in each reactor 31, 32.

[0040] In the chemical looping reactor 22, the gas temperature inside the first reactor 31 (i.e., the reactor where carbon dioxide reduction is performed) is, for example, 450 to 1000°C, preferably 500 to 850°C. The gas temperature inside the second reactor 32 (i.e., the reactor where hydrogen oxidation is performed) is, for example, 300 to 800°C, preferably 300 to 750°C. The reactors 31 and 32 do not need to be heated, but may be heated if the gas temperatures of carbon dioxide and hydrogen supplied thereto do not reach the above temperatures.

[0041] As the catalyst circulated between the reactors 31, 32 via the catalyst forward path 33 and the catalyst return path 34, a known metal oxide catalyst can be used, and examples thereof include oxides of one or more metals selected from La, Sr, Co, Ce, Zr, Y, and Fe.

[0042] A first heater 35 and a second heater 36 are disposed between the chemical looping reactor 22 and the solid carbonization reactor 4. The first heater 35 is connected to the first reactor 31 via a process gas line 42. The first heater 35 and the second heater 36 are connected via a process gas line 43. The second heater 36 and the solid carbonization reactor 4 are connected via a process gas line 44. The solid carbonization reactor 4 and the gas treatment device 5 are connected via a process gas line 45.

[0043] The second reactor 32 and the treated gas line 42 are connected via a third hydrogen supply line 46, and of the hydrogen supplied from the hydrogen storage and supply device 13 to the second reactor 32 via the second hydrogen supply line 14, hydrogen that is not used in the oxidation reaction in the second reactor 32 is introduced into the treated gas line 42 via the third hydrogen supply line 46 and mixed with the treated gas flowing through the treated gas line 42.

[0044] <First heater> The first heater 35 has an off-gas inlet and an off-gas outlet, respectively, for introducing and discharging the off-gas from the solid carbonization reaction apparatus 4. The off-gas inlet of the first heater 35 is connected to a treatment gas line 45 via an off-gas line 37. The off-gas outlet of the first heater 35 is connected to a treatment gas line 41 between the carbon dioxide capture apparatus 21 and the chemical looping reaction apparatus 22 (first reactor 31), which are disposed on the gas flow upstream side of the solid carbonization reaction apparatus 4, via an off-gas line 38. The first heater 35 is mainly configured as a heat exchanger that introduces the off-gas from the solid carbonization reaction apparatus 4 via the off-gas line 37 as a heat medium and exchanges heat between the introduced off-gas and treatment gas flowing from the treatment gas line 42 to the treatment gas line 43. The first heater 35 uses the introduced off-gas as a heat source and heats the treatment gas flowing from the treatment gas line 42 to the treatment gas line 43. In this embodiment, the off-gas line 37 and the off-gas line 38 constitute an off-gas introduction path 40 that introduces the off-gas from the solid carbonization reaction device 4 to the upstream side of the gas flow of the solid carbonization reaction device 4.

[0045] <Second heater> The second heater 36 is mainly composed of a heat exchanger that heats the process gas flowing from the process gas line 43 to the process gas line 44 to a predetermined temperature by heat exchange with a heat medium. As the heat medium used here, part or all of the combustion exhaust gas that is normally discharged into the atmosphere and discarded can be used. In this way, energy costs can be kept low by effectively utilizing the waste heat of the exhaust gas that is normally discharged into the atmosphere and discarded.

[0046] <Cooler> A cooler 39 is provided in the off-gas line 38. The cooler 39 is mainly composed of a heat exchanger that exchanges heat between the off-gas flowing through the off-gas line 38 and a heat medium. Here, the heat medium may be, for example, air or cooling water. The cooler 39 has the function of cooling the off-gas flowing through the off-gas line 38, condensing the moisture contained in the off-gas, and discharging the condensed water. The off-gas from which the moisture has been removed by the cooler 39 is introduced via the off-gas line 38 into a treated gas line 41 between the carbon dioxide capture device 21 and the chemical looping reactor 22 (first reactor 31), which are disposed on the gas flow upstream side of the solid carbonization reactor 4, and is mixed with the treated gas flowing through the treated gas line 41.

[0047] The first heater 35 and the second heater 36 are not limited to the example shown in FIG. 1 in which they are arranged between the chemical looping reactor 22 and the solid carbonization reactor 4, but may be arranged between the carbon dioxide capture unit 21 and the chemical looping reactor 22 (first reactor 31).

[0048] <Solid carbonization reactor> The solid carbonization reactor 4 converts the carbon monoxide produced by the carbon monoxide production means 3A into carbon through a solid carbonization reaction represented by the following formula (1), and also produces carbon dioxide as a by-product. 2CO → C + CO2 (1)

[0049] The solid carbonization reactor 4 is a reactor filled with a catalyst (e.g., an iron-based metal catalyst) that promotes the reaction (1) above, and both reduction and oxidation of carbon monoxide are carried out inside the reactor. In the solid carbonization reactor 4, carbon is deposited on the catalyst surface inside the reactor by passing carbon monoxide through the reactor. The gas temperature inside the solid carbonization reactor 4 is, for example, 300 to 1000°C, preferably 450 to 850°C (approximately 500°C in this example). As described above, the treatment gas supplied to the solid carbonization reactor 4 is preheated by the first heater 35 and the second heater 36. Therefore, there are cases where it is not necessary to heat the catalyst inside the solid carbonization reactor 4 using a heating furnace or the like, but a configuration in which the catalyst is heated using a heating furnace or the like may be adopted as necessary.

[0050] In the solid carbonization equipment 1A, the process gas flowing from the process gas line 42 to the solid carbonization reactor 4 via the process gas lines 43 and 44 is heated by the first heater 35 through heat exchange with the off-gas from the solid carbonization reactor 4, and is also heated by the second heater 36 through heat exchange with waste heat, etc. This makes it possible to reduce the thermal energy required for heating when reducing carbon monoxide to carbon in the solid carbonization reactor 4, thereby reducing energy costs.

[0051] In the solid carbonization equipment 1A, a portion of the off-gas containing unreacted gases (CO, CO2, H2) and by-product carbon dioxide from the solid carbonization reactor 4 is mixed with the treatment gas flowing through the treatment gas line 41 upstream of the chemical looping reactor 22. By recycling the off-gas containing unreacted gases and by-product carbon dioxide again as a raw material for solid carbon in this way, the yield of solid carbonization can be improved and the amount of carbon dioxide that is wasted and discharged without being solid carbonized can be reduced. The remainder of the off-gas from the solid carbonization reactor 4 is introduced into the gas treatment device 5 via the treatment gas line 45 and treated to be rendered harmless.

[0052] In the solid carbonization facility 1A, hydrogen produced by electrolyzing water in the water electrolysis device 11 is produced using electricity supplied via power supply lines 15 and 16, i.e., electricity generated using the heat of combustion exhaust gas and / or electricity generated using renewable energy. In this way, hydrogen for reduction is produced without using electricity generated using a separate fossil fuel and without emitting additional carbon dioxide. This can contribute to reducing carbon dioxide emissions.

[0053] The controller 6 is mainly composed of a computer and has functional parts, namely, a measuring part 50, a concentration ratio calculation part 51, and a valve control part 52, and is configured so that the functions of each functional part are performed by executing a predetermined program.

[0054] <Means for measuring hydrogen concentration> The hydrogen concentration measuring means 7 includes a measuring unit 50 and a hydrogen concentration meter 53. The hydrogen concentration meter 53 detects the concentration of hydrogen contained in the process gas flowing through the process gas line 44, and outputs a detection signal corresponding to the hydrogen concentration. The detection signal from the hydrogen concentration meter 53 is sent to the controller 6. Then, based on the detection signal from the hydrogen concentration meter 53, the measuring unit 50 measures the concentration of hydrogen contained in the process gas introduced into the solid carbonization reaction device 4 via the process gas line 44.

[0055] <Mechanism for measuring carbon monoxide concentration> The carbon monoxide concentration measuring means 8 includes a measuring unit 50 and a carbon monoxide concentration meter 54. The carbon monoxide concentration meter 54 detects the concentration of carbon monoxide contained in the process gas flowing through the process gas line 44, and outputs a detection signal corresponding to the carbon monoxide concentration. The detection signal from the carbon monoxide concentration meter 54 is sent to the controller 6. Then, based on the detection signal from the carbon monoxide concentration meter 54, the measuring unit 50 measures the concentration of carbon monoxide contained in the process gas introduced into the solid carbonization reaction device 4 via the process gas line 44.

[0056] <Control means> Control means 60 that controls the hydrogen supply means 2 includes a flow control valve 61 interposed in the second hydrogen supply line 14, a valve control unit 52 that controls the valve opening degree of the flow control valve 61, and a flow meter 62 interposed in the second hydrogen supply line 14 between the hydrogen storage and supply device 13 and the flow control valve 61. Control means 60 controls the hydrogen supply means 2 so that the ratio (A / B) of the hydrogen concentration (A%) measured by the hydrogen concentration measurement means 7 to the carbon monoxide concentration (B%) measured by the carbon monoxide concentration measurement means 8 is 0.05 to 2.0. Specific control details will be described later.

[0057] In the solid carbonization equipment 1A configured as described above, the following processes are performed: a carbon dioxide recovery process, a water electrolysis process, a hydrogen supply process, a first heating process, a second heating process, a chemical looping reaction process, a solid carbonization reaction process, and a cooling process.

[0058] <Carbon dioxide capture process> The carbon dioxide capture step is carried out by introducing the combustion exhaust gas discharged from the incinerator of the waste combustion treatment facility 10 and having been subjected to dust removal and hazardous substance removal treatments into the carbon dioxide capture device 21 via the exhaust gas supply line 23, then introducing it into an absorption tower containing, for example, an amine-based absorption liquid to bring it into contact with the absorption liquid, sending the absorption liquid that has absorbed the carbon dioxide contained in the combustion exhaust gas from the absorption tower to a regeneration tower, and stripping and capturing the carbon dioxide from the absorption liquid in the regeneration tower. The treated gas containing carbon dioxide from the carbon dioxide capture device 21 is introduced into the first reactor 31 via the treated gas line 41.

[0059] <Water electrolysis process> The water electrolysis step is performed by electrolyzing water in the water electrolysis device 11 using electric power supplied via the electric power supply lines 15 and 16. In this way, the hydrogen used for reduction in the subsequent chemical looping reaction step is produced without using electric power separately generated using fossil fuels and without emitting any additional carbon dioxide, thereby contributing to carbon dioxide reduction.

[0060] <Hydrogen supply process> In the water electrolysis process, hydrogen produced by electrolysis of water is supplied to and temporarily stored in hydrogen storage and supply device 13 via first hydrogen supply line 12. The hydrogen stored in hydrogen storage and supply device 13 is supplied to second reactor 32 via second hydrogen supply line 14, and is also supplied from second reactor 32 to treatment gas line 42 via third hydrogen supply line 46, where it is mixed with treatment gas containing carbon monoxide and the like from first reactor 31. The treatment gas is then introduced into first heater 35.

[0061] <First heating step> The first heating step is performed by introducing the treatment gas flowing from the treatment gas line 42 to the treatment gas line 43 into the first heater 35, and introducing the off-gas from the solid carbonization reaction device 4 via the off-gas line 37 into the first heater 35, and by exchanging heat between the introduced treatment gas and the off-gas.

[0062] <Second heating process> The second heating step is performed by introducing the process gas heated in the first heater 35 into the second heater 36, and also introducing a heat medium that functions as a heat source into the second heater 36, and then exchanging heat between the introduced process gas and the heat medium (e.g., combustion exhaust gas). In the second heater 36, the process gas is heated to a predetermined temperature.

[0063] <Chemical Looping Reaction Process> The chemical looping reaction step is carried out by introducing a gas containing hydrogen supplied from the hydrogen supply means 2 and a gas containing carbon dioxide recovered by the carbon dioxide recovery device 21, and utilizing a chemical looping reaction. Carbon monoxide and water (water vapor) are produced by this chemical looping reaction step.

[0064] <Solid carbonization reaction process> The solid carbonization reaction step is carried out by introducing the treated gas containing carbon monoxide produced in the chemical looping reaction step into the solid carbonization reactor 4, and proceeding with the reaction represented by the above formula (1) due to the reduction and oxidation of carbon monoxide inside the reactor. In the solid carbonization reaction step, carbon monoxide is converted to carbon by the action of the catalyst, and carbon is deposited on the surface of the catalyst inside the solid carbonization reactor 4. The deposited carbon is recovered as solid carbon.

[0065] <Cooling process> The cooling step is performed by introducing the off-gas flowing through the off-gas line 38 into the cooler 39, introducing a heat medium that functions as a cold heat source into the cooler 39, and exchanging heat between the introduced off-gas and the heat medium. The process gas is cooled to a predetermined temperature in the cooler 39. At this time, condensed water generated by condensation of moisture contained in the off-gas is discharged. The off-gas from which moisture has been removed by the cooler 39 is introduced into the process gas line 41 via the off-gas line 38 and mixed with the process gas flowing through the process gas line 41.

[0066] Incidentally, the concentrations of gas components contained in the treated gas may fluctuate depending on the operating conditions of the waste incineration treatment facility 10, etc. Even if such fluctuations occur, the control for adjusting the concentrations of hydrogen and carbon monoxide in the treated gas to a ratio suitable for the solid carbonization reaction will be described below.

[0067] Fig. 2 is a graph showing the relationship between the conversion rate of carbon monoxide to solid carbon (solid carbonization reaction rate) and the concentration ratio of hydrogen and carbon monoxide. When the ratio (A / B) of the hydrogen concentration (A%) to the carbon monoxide concentration (B%) shown on the horizontal axis of the graph in Fig. 2 is in the range of 0.05 to 2.0, the solid carbonization reaction rate shown on the vertical axis of the graph in Fig. 2 exhibits a high value. Therefore, in order to maintain a high level of the solid carbonization reaction rate, a hydrogen supply amount control step is performed in which the amount of hydrogen supplied by the hydrogen supply means 2 is controlled so that the concentration ratio (A / B) is 0.05 to 2.0. Note that if the concentration ratio (A / B) exceeds 2.0, undesirable reactions that consume a large amount of carbon monoxide occur, and therefore the upper limit of the concentration ratio (A / B) is 2.0.

[0068] 3 is a flowchart showing the procedure of the hydrogen supply amount control process. In FIG. 3, the symbol "S" represents a step. The hydrogen supply amount control process will be described below (see FIGS. 1 and 3).

[0069] <Steps S1 to S2> The measurement unit 50 receives detection signals from the hydrogen concentration meter 53 and the carbon monoxide concentration meter 54 (S1). Based on the received detection signals, the measurement unit 50 measures the concentration of hydrogen in the treatment gas using the hydrogen concentration meter 53 and measures the concentration of carbon monoxide in the treatment gas using the carbon monoxide concentration meter 54 (S2).

[0070] <Steps S3 to S5> The concentration ratio calculation unit 51 calculates the concentration ratio (A / B) between the measured hydrogen concentration (A%) and the measured carbon monoxide concentration (B%) (S3). If the calculated concentration ratio (A / B) is less than 0.05 or exceeds 2.0 ("YES" in step S4), the valve control unit 52 calculates a target value for the amount of hydrogen to be supplied by the hydrogen supply means 2 so that the concentration ratio (A / B) is 0.05 to 2.0, for example, 0.5 (not limited to 0.5), which is the concentration ratio (A / B) corresponding to the highest solid carbonization reaction rate (S5).

[0071] <Steps S6 to S7> Then, the valve control unit 52 uses the detection signal of the flow meter 62 as a feedback signal to output a control signal to the flow control valve 61, thereby controlling the valve opening degree of the flow control valve 61 so that the actual amount of hydrogen supplied by the hydrogen supply means 2, i.e., the amount of hydrogen supplied from the hydrogen storage and supply device 13 to the second reactor 32 via the second hydrogen supply line 14, reaches the target value calculated in step S5.

[0072] In this way, even if the concentrations of gas components (hydrogen, carbon monoxide) contained in the process gas fluctuate, the concentrations of hydrogen and carbon monoxide in the process gas can be adjusted to a ratio (0.05 to 2.0) suitable for the solid carbonization reaction. Therefore, the solid carbonization reaction rate can be maintained at a high level, and solid carbon can be produced with high efficiency.

[0073] Second Embodiment 4 is a block diagram showing a schematic configuration of a solid carbonization facility 1B according to a second embodiment of the present invention. In the second embodiment, components that are the same as or similar to those in the first embodiment are simply given the same reference numerals in the drawings, and detailed descriptions thereof will be omitted. The following description will focus on the parts unique to the second embodiment (the same applies to a third embodiment and modified examples 1 and 2 of the first embodiment, which will be described later).

[0074] In the solid carbonization equipment 1A of the second embodiment shown in Fig. 1, the carbon monoxide generation means 3A is mainly composed of a carbon dioxide capture device 21 and a chemical looping reactor 22, whereas in the solid carbonization equipment 1B of the second embodiment shown in Fig. 4, the carbon monoxide generation means 3B is mainly composed of a carbon dioxide capture device 21 and a carbon dioxide electrolysis device 70. Other than that, the configuration is the same as that of the solid carbonization equipment 1A of the first embodiment. Therefore, the solid carbonization equipment 1B of the second embodiment can also obtain basically the same effects as those of the solid carbonization equipment 1A of the first embodiment.

[0075] <Carbon dioxide electrolysis device> The carbon dioxide electrolysis device 70 receives a carbon dioxide-containing treatment gas from the carbon dioxide recovery device 21 via a treatment gas line 41 and electrolyzes the carbon dioxide contained in the treatment gas to produce carbon monoxide. The carbon dioxide electrolysis device 70 of this embodiment may include, for example, a solid polymer carbon dioxide electrolysis cell configured to electrolyze carbon dioxide at room temperature and pressure to produce carbon monoxide. The carbon dioxide electrolysis cell includes a cathode (negative electrode) having a gas diffusion layer and a catalyst layer, a solid polymer membrane, and an anode (positive electrode). When an external voltage is applied to the carbon dioxide electrolysis cell while supplying a carbon dioxide-containing treatment gas and an electrolytic solution, a reduction reaction of carbon dioxide proceeds on the cathode side, producing carbon monoxide and hydroxide ions.

[0076] Third Embodiment Fig. 5 is a block diagram showing a schematic configuration of a solid carbonization facility 1C according to a third embodiment of the present invention. In the solid carbonization facility 1C of the third embodiment shown in Fig. 5, a carbon monoxide generation means 3C is mainly composed of a carbon dioxide capture device 21 and a reverse shift reactor 80. The rest of the configuration is the same as that of the solid carbonization facility 1A of the first embodiment. Therefore, the solid carbonization facility 1C of the third embodiment can also basically obtain the same effects as those of the solid carbonization facility 1A of the first embodiment.

[0077] <Reverse shift reactor> Here, the reverse shift reactor 80 receives carbon dioxide in the treated gas heated by the heaters 35, 36 and hydrogen from the hydrogen supply means 2, and produces carbon monoxide and water from the carbon dioxide and hydrogen through the reverse shift reaction shown in the following formula (2). CO2 + H2 → CO + H2O (2)

[0078] The reverse shift reactor 80 is a reactor filled with a catalyst (e.g., a copper-based metal catalyst) that promotes the reaction represented by the above formula (2). Both carbon dioxide reduction and hydrogen oxidation occur within the reactor. In the reverse shift reactor 80, carbon dioxide and hydrogen are passed through the reactor, generating carbon monoxide and water (water vapor). The carbon monoxide and water (water vapor) are then discharged from the reactor. The gas temperature within the reverse shift reactor 80 is, for example, 300 to 1000°C, preferably 450 to 850°C (approximately 500°C in this example). As described above, the process gas supplied to the reverse shift reactor 80 is preheated by the heaters 35 and 36. Therefore, it may not be necessary to heat the catalyst within the reverse shift reactor 80 using a heating furnace or the like. However, a configuration in which the catalyst is heated using a heating furnace or the like may be adopted as necessary.

[0079] The solid carbonization equipment of the present invention has been described above based on a number of embodiments, but the present invention is not limited to the configurations described in the above embodiments, and the configuration can be changed as appropriate within the scope of the spirit of the invention, such as by appropriately combining the configurations described in the respective embodiments.

[0080] (Modification (1) of the first embodiment) FIG. 6 is a block diagram showing a schematic configuration of a modified example (1) of the solid carbonization equipment 1A according to the first embodiment of the present invention. In the solid carbonization equipment 1A shown in FIG. 1, the hydrogen concentration measurement means 7 includes a measurement unit 50 and a hydrogen concentration meter 53, and is configured to directly measure the concentration of hydrogen contained in the process gas based on the detection result of the hydrogen concentration meter 53. In contrast, in the modified example (1) of the solid carbonization equipment 1A shown in FIG. 6, the hydrogen concentration measurement means 7′ includes the measurement unit 50, an upstream flow meter 91, and a downstream flow meter 92, and is configured to indirectly measure the concentration of hydrogen contained in the process gas based on the detection results of the upstream flow meter 91 and the downstream flow meter 92. Here, the upstream flow meter 91 detects the flow rate of gas flowing upstream of the solid carbonization reaction device 4. Meanwhile, the downstream flow meter 92 detects the flow rate of gas flowing downstream of the solid carbonization reaction device 4.

[0081] The hydrogen concentration can be indirectly determined as follows. That is, if the difference (change in flow rate) between the gas flow rate on the upstream side of the gas flow in the solid carbonization reactor 4 and the gas flow rate on the downstream side of the gas flow in the solid carbonization reactor 4 is determined, the conversion rate of carbon monoxide to solid carbon in the solid carbonization reactor 4 can be determined. If the conversion rate of carbon monoxide to solid carbon is known, a predicted value (estimated value) of the hydrogen concentration can be determined by referring to relationship data between the conversion rate of carbon monoxide to solid carbon and the hydrogen concentration value relative to carbon monoxide, which has been obtained in advance through experiments, etc. Therefore, in the hydrogen concentration measurement means 7', the measurement unit 50 determines the difference in gas flow rate between the upstream side and the downstream side of the solid carbonization reactor 4 based on the detection signals of the upstream flow meter 91 and the downstream flow meter 92, determines the conversion rate of carbon monoxide to solid carbon based on the determined gas flow rate difference, and determines the predicted value of the hydrogen concentration by referring to the relationship data, which is then calculated as the measured value.

[0082] In this modification (1), the hydrogen supply amount control step is performed as follows (see the flowchart in FIG. 3).

[0083] <Steps S1 to S2> The measurement unit 50 receives detection signals from the upstream flow meter 91, the downstream flow meter 92, and the carbon monoxide concentration meter 54 (S1). Based on the received detection signals, the measurement unit 50 measures the concentration of hydrogen in the treatment gas using the upstream flow meter 91 and the downstream flow meter 92 as described above, and also measures the concentration of carbon monoxide in the treatment gas using the carbon monoxide concentration meter 54 (S2).

[0084] <Steps S3 to S5> The concentration ratio calculation unit 51 calculates the concentration ratio (A / B) between the measured hydrogen concentration (A%) and the measured carbon monoxide concentration (B%) (S3). If the calculated concentration ratio (A / B) is less than 0.05 or exceeds 2.0 ("YES" in step S4), the valve control unit 52 calculates a target value for the amount of hydrogen to be supplied by the hydrogen supply means 2 so that the concentration ratio (A / B) is 0.05 to 2.0, for example, 0.5 (not limited to 0.5), which is the concentration ratio (A / B) corresponding to the highest solid carbonization reaction rate (S5).

[0085] <Steps S6 to S7> Then, the valve control unit 52 uses the detection signal of the flow meter 62 as a feedback signal to output a control signal to the flow control valve 61, thereby controlling the valve opening degree of the flow control valve 61 so that the actual amount of hydrogen supplied by the hydrogen supply means 2, i.e., the amount of hydrogen supplied from the hydrogen storage and supply device 13 to the second reactor 32 via the second hydrogen supply line 14, reaches the target value calculated in step S5.

[0086] In this way, even if the concentrations of gas components (hydrogen, carbon monoxide) contained in the process gas fluctuate, the concentrations of hydrogen and carbon monoxide in the process gas can be adjusted to a ratio (0.05 to 2.0) suitable for the solid carbonization reaction. Therefore, the solid carbonization reaction rate can be maintained at a high level, and solid carbon can be produced with high efficiency.

[0087] Note that the above variant example (1) is an example in which a hydrogen concentration measuring means 7' that indirectly measures hydrogen concentration is applied to the solid carbonization equipment 1A of the first embodiment, but it goes without saying that the hydrogen concentration measuring means 7' can also be applied to each of the solid carbonization equipment 1B of the second embodiment and the solid carbonization equipment 1C of the third embodiment.

[0088] (Modification (2) of the first embodiment) 7 is a block diagram showing a schematic configuration of a modified example (2) of the solid carbonization equipment 1A according to the first embodiment of the present invention. In the first embodiment and its modified example (1), the concentration ratio (A / B) of the hydrogen concentration (A%) to the carbon monoxide concentration (B%) is calculated based on the measurement results of the hydrogen concentration measuring means 7, 7' and the carbon monoxide concentration measuring means 8. In contrast, in the modified example (2) of the solid carbonization equipment 1A shown in FIG. 7, the concentration ratio (A / B) is calculated based on the conversion rate of carbon monoxide to solid carbon obtained from the detection results of the upstream flow meter 91 and the downstream flow meter 92.

[0089] 8 is a flowchart showing the procedure of the hydrogen supply amount control process in the modified example (2) of the first embodiment. The hydrogen supply amount control process in the modified example (2) will be described below.

[0090] <Steps S1 to S4> The measurement unit 50 receives detection signals from the upstream flow meter 91 and the downstream flow meter 92 (S1). The measurement unit 50 measures and determines the difference in gas flow rate between the upstream side and the downstream side in the solid carbonization reaction device 4 based on the detection signals from the upstream flow meter 91 and the downstream flow meter 92 (S2). The concentration ratio calculation unit 51 determines the conversion rate of carbon monoxide to solid carbon based on the measured gas flow rate difference (S3). The concentration ratio calculation unit 51 then calculates the concentration ratio (A / B) by referring to the relationship data between the conversion rate of carbon monoxide to solid carbon and the concentration ratio of hydrogen and carbon monoxide shown in the graph of Fig. 2.

[0091] <Steps S5 to S6> If the calculated concentration ratio (A / B) is less than 0.05 or exceeds 2.0 ("YES" in step S5), the valve control unit 52 calculates a target value for the amount of hydrogen to be supplied by the hydrogen supply means 2 so that the concentration ratio (A / B) is 0.05 to 2.0, and here, as an example, the concentration ratio (A / B) is 0.5 (not limited to 0.5) corresponding to the highest solid carbonization reaction rate (S6).

[0092] <Steps S7 to S8> Then, the valve control unit 52 uses the detection signal of the flow meter 62 as a feedback signal to output a control signal to the flow control valve 61, thereby controlling the valve opening of the flow control valve 61, so that the actual amount of hydrogen supplied by the hydrogen supply means 2, i.e., the amount of hydrogen supplied from the hydrogen storage and supply device 13 to the second reactor 32 via the second hydrogen supply line 14, reaches the target value calculated in step S6.

[0093] In this way, even if the concentrations of gas components (hydrogen, carbon monoxide) contained in the process gas fluctuate, the concentrations of hydrogen and carbon monoxide in the process gas can be adjusted to a ratio (0.05 to 2.0) suitable for the solid carbonization reaction. Therefore, the solid carbonization reaction rate can be maintained at a high level, and solid carbon can be produced with high efficiency.

[0094] The above variant example (2) is an example in which a configuration for calculating the concentration ratio (A / B) based on the conversion rate of carbon monoxide to solid carbon obtained from the difference in gas flow rate between the upstream and downstream sides of the solid carbonization reaction device 4 is applied to the solid carbonization equipment 1A of the first embodiment, but it goes without saying that a similar configuration can also be applied to each of the solid carbonization equipment 1B of the second embodiment and the solid carbonization equipment 1C of the third embodiment.

[0095] In the first to third embodiments, a configuration including the concentration ratio calculation unit 51, the hydrogen concentration measurement means 7, and the carbon monoxide concentration measurement means 8 corresponds to the "concentration ratio calculation means" in the present invention. In the modified example (1) of the first embodiment, a configuration including the concentration ratio calculation unit 51, the hydrogen concentration measurement means 7', and the carbon monoxide concentration measurement means 8 corresponds to the "concentration ratio calculation means" in the present invention. In the modified example (2) of the first embodiment, a configuration including the measurement unit 50, the concentration ratio calculation unit 51, the upstream flow meter 91, and the downstream flow meter 92 corresponds to the "concentration ratio calculation means" in the present invention. [Industrial Applicability]

[0096] The solid carbonization equipment of the present invention can be used in applications such as producing solid carbon from carbon dioxide contained in exhaust gas generated by the combustion of fossil fuels in thermal power plants, steel mills, oil refineries, etc.; carbon dioxide contained in exhaust gas generated by the combustion of off-gas in hydrogen production facilities; carbon dioxide contained in exhaust gas generated by the combustion of waste in municipal waste incineration facilities; and carbon dioxide contained in exhaust gas generated by the combustion of biomass fuels in biomass power generation facilities. [Explanation of symbols]

[0097] 1A~1C Solid carbonization equipment 2. Hydrogen supply means 3A~3C Carbon monoxide generation means 4. Solid carbonization reactor 7,7´ Hydrogen concentration measurement means 8 Carbon monoxide concentration measurement means 21 Carbon dioxide capture equipment 22 Chemical Looping Reactor 36 Second heater 40 Off-gas inlet 53 Hydrogen concentration meter 60 Control Means 70 Carbon dioxide electrolysis device 80 Reverse shift reactor 91 Upstream flow meter 92 Downstream flow meter

Claims

1. a hydrogen supply means for supplying hydrogen; carbon monoxide generating means for generating carbon monoxide; a solid carbonization reactor having a catalyst for reducing and oxidizing carbon monoxide, into which hydrogen supplied from the hydrogen supply means and a gas containing carbon monoxide generated by the carbon monoxide generation means are introduced and which precipitates solid carbon by the action of the catalyst; a concentration ratio calculation means for calculating a concentration ratio (A / B) between a concentration (A%) of hydrogen contained in the gas introduced into the solid carbonization reactor and a concentration (B%) of carbon monoxide contained in the gas; a control means for controlling the hydrogen supply means so that the concentration ratio (A / B) calculated by the concentration ratio calculation means is 0.05 to 2.0; Solid carbonization equipment equipped with:

2. The carbon monoxide generating means is a carbon dioxide recovery device that recovers carbon dioxide contained in the combustion exhaust gas; a chemical looping reactor into which the hydrogen-containing gas supplied from the hydrogen supply means and the carbon dioxide-containing gas recovered by the carbon dioxide recovery unit are introduced and which generates carbon monoxide by utilizing a chemical looping reaction; The solid carbonization facility according to claim 1, comprising:

3. The carbon monoxide generating means is a carbon dioxide recovery device that recovers carbon dioxide contained in the combustion exhaust gas; a carbon dioxide electrolysis device that electrolyzes the carbon dioxide recovered by the carbon dioxide recovery device to generate carbon monoxide; The solid carbonization facility according to claim 1, comprising:

4. The carbon monoxide generating means is a carbon dioxide recovery device that recovers carbon dioxide contained in the combustion exhaust gas; a reverse shift reactor into which a gas containing hydrogen supplied from the hydrogen supply means and carbon dioxide recovered by the carbon dioxide recovery unit is introduced, and which reduces the carbon dioxide in the gas by a reverse shift reaction to produce carbon monoxide; The solid carbonization facility according to claim 1, comprising:

5. The solid carbonization facility according to any one of claims 1 to 4, further comprising a heater that heats the gas flowing upstream of the solid carbonization reactor by heat exchange with the off-gas from the solid carbonization reactor.

6. The solid carbonization facility according to any one of claims 1 to 4, further comprising an off-gas introduction passage for introducing off-gas from the solid carbonization reactor into the upstream side of the gas flow of the solid carbonization reactor.

7. The concentration ratio calculation means a hydrogen concentration measuring means for measuring the concentration of hydrogen contained in the gas introduced into the solid carbonization reactor; a carbon monoxide concentration measuring means for measuring the concentration of carbon monoxide contained in the gas introduced into the solid carbonization reactor; Including, 2. The solid carbonization facility according to claim 1, wherein the concentration ratio (A / B) is calculated based on the hydrogen concentration (A%) measured by the hydrogen concentration measuring means and the carbon monoxide concentration (B%) measured by the carbon monoxide concentration measuring means.

8. The hydrogen concentration measuring means a hydrogen concentration meter for detecting the concentration of hydrogen contained in the gas introduced into the solid carbonization reactor, 8. The solid carbonization facility according to claim 7, wherein the concentration of hydrogen contained in the gas introduced into the solid carbonization reactor is measured based on the detection result of the hydrogen concentration meter.

9. The hydrogen concentration measuring means an upstream flow meter for detecting a flow rate of gas flowing upstream of the solid carbonization reactor; a downstream flow meter for detecting a flow rate of gas flowing downstream of the solid carbonization reactor; Including, The solid carbonization facility according to claim 7 , wherein the concentration of hydrogen contained in the gas introduced into the solid carbonization reactor is measured based on the detection results of the upstream flow meter and the downstream flow meter.

10. The concentration ratio calculation means an upstream flow meter for detecting a flow rate of gas flowing upstream of the solid carbonization reactor; a downstream flow meter for detecting a flow rate of gas flowing downstream of the solid carbonization reactor; Including, 2. The solid carbonization facility according to claim 1, wherein the concentration ratio (A / B) is calculated based on a conversion rate of carbon monoxide to solid carbon determined from detection results of the upstream flow meter and the downstream flow meter.

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