KR20200055939A - Manufacturing method for carbon monoxide by chemical looping combustion - Google Patents

Abstract

The present invention relates to a method for manufacturing carbon monoxide by using chemical looping combustion and, more particularly, to a method for manufacturing carbon monoxide from carbon dioxide using oxygen transfer particles.

Description

Manufacturing method of carbon monoxide by chemical roofing combustion {MANUFACTURING METHOD FOR CARBON MONOXIDE BY CHEMICAL LOOPING COMBUSTION}

The present invention relates to a method for producing carbon monoxide using chemical roofing combustion, and more particularly, to a method for producing carbon monoxide from carbon dioxide using oxygen transfer particles.

As the average temperature of the earth rises due to the greenhouse effect caused by the increase in the concentration of carbon dioxide in the atmosphere, the damage of climate change continues to appear. Accordingly, there is a need for a new technology for producing carbon monoxide, a reaction intermediate capable of separating carbon dioxide at the source and capturing and storing (Carbon Capture and Storage: CCS) or synthesizing useful chemicals through conversion of carbon dioxide.

The carbon monoxide is used in hospitals for therapeutic purposes or as a laser-generating medium, and is used in various fields such as industrial production of acetic acid, production of metal carbonyls, production of biodiesel, and production of polymer plastics such as polyketones. .

As a conventional method for producing carbon monoxide, a carbon dioxide gasification method using coal (C + CO ₂ = CO), a method using steam reforming (C + H ₂ O = H ₂ + CO), incomplete combustion The method used (2C + O ₂ = 2CO), the method using high-temperature electrolysis of carbon dioxide (2CO ₂ = 2CO + O ₂ ), and the method produced during the smelting process of metal oxide ore (C + MO = M + CO) have.

However, the gasification method requires additional equipment and processes to remove impurities other than carbon in coal, such as denitrification equipment and desulfurization equipment, and in the case of the high temperature electrolysis method, the membrane used for electrolysis is expensive and the production cost is high. There is a high problem, there is a need for the development of carbon monoxide production technology that is inexpensive and capable of mass production.

Meanwhile, chemical looping combustion (CLC) is a technology capable of separating carbon dioxide from fuel at a high concentration, and circulating a metal oxide containing oxygen-transfer particles using two reactors in which oxidation and reduction reactors are individually configured. It is a technique to do.

The oxygen transfer particles are solid oxides that exchange oxygen while circulating the oxidation and reduction reactors during the combustion of chemical roofing in the form of metal oxides or metals, and are also called oxygen carrier particles.

During chemical roofing combustion, air is generally injected into the oxidation reactor, and hydrocarbons such as coal, biomass, synthetic gas, natural gas, and LPG are injected into the reduction reactor.

More specifically, in the oxidation reactor, the oxygen transfer particles react with oxygen in the air to form an oxide, and the resulting oxide moves to a reduction reactor. In addition, in the reduction reactor, the shifted oxide reacts with the fuel to generate carbon dioxide and water vapor, and the oxide is reduced again and circulated to the oxidation reactor.

However, conventional chemical roofing combustion has a problem in that carbon dioxide and air pollutant nitrogen oxides, which cause a greenhouse effect, are generated because the fuel and air are directly contacted and burned. In particular, research related to the production of carbon monoxide using chemical roofing combustion This is insignificant.

Republic of Korea Patent Registration No. 10-1594799

An object of the present invention is to provide a method for producing carbon monoxide from hydrogen and carbon dioxide using chemical roofing combustion.

The present invention for achieving the above object relates to a method for producing carbon monoxide from carbon dioxide by using oxygen transfer particles.

Specifically, one aspect of the invention a) the MFe _x O _y is reacted with hydrogen in the step of reducing the MFe _x O _y; And b) reacting the reduced MFe _x O _y with carbon dioxide to produce carbon monoxide; including, a method for producing carbon monoxide by chemical roofing combustion.

In one aspect of the present invention, the MFe _x O _y may be characterized by being MgFe ₂ O ₄ .

In one aspect of the present invention, steps a) and b) may be repeated sequentially.

In one embodiment of the present invention, MFe _x O _y reduced in step b) may be oxidized and regenerated as oxygen transfer particles.

In one aspect of the present invention, the method for producing the carbon monoxide may be performed using a fixed bed reactor or a fluidized bed reactor.

In one embodiment of the present invention, after the step b) may be further comprising a carbon monoxide separation step.

In one aspect of the present invention, steps a) and b) may be performed independently of each other in a temperature range of 500 to 1,500 ° C.

In one aspect of the present invention, the maximum conversion rate of the carbon dioxide may be 70% or more.

In one embodiment of the present invention, the maximum selectivity of the carbon monoxide may be 70% or more.

The method for producing carbon monoxide by chemical roofing combustion according to the present invention has the advantage that, as hydrogen and carbon dioxide are used as fuels, there is no generation of nitrogen oxide harmful substances, which are by-products of the conventional chemical roofing combustion reaction.

In addition, the carbon monoxide production method according to the present invention, by using carbon dioxide as a greenhouse gas, it is possible to resource of carbon dioxide and has an effect of preventing the greenhouse effect.

In addition, the method for producing carbon monoxide according to the present invention has the advantage of being capable of mass production of high-purity carbon monoxide using a simple process and equipment, and miniaturization of equipment.

In addition, the method for producing carbon monoxide according to the present invention has an advantage in that the carbon dioxide conversion rate of the oxygen transfer particles used in the production of carbon monoxide is excellent, and the carbon monoxide selectivity is high.

In addition, in the method for producing carbon monoxide according to the present invention, as the oxygen transport particles and fuel gas used are inexpensive, it is possible to produce high value-added carbon monoxide through raw materials at low manufacturing cost.

1 is a schematic diagram of a method for producing carbon monoxide according to an aspect of the present invention.
2 is an XRD graph of MFe _x O _y prepared according to an embodiment of the present invention.
3 is a FE-SEM photograph of MFe _x O _y prepared according to an embodiment of the present invention.
4 is a gas analysis result of MgFe ₂ O ₄ according to an embodiment of the present invention.
5 is a gas analysis result of CuFe ₂ O ₄ according to an embodiment of the present invention.

Hereinafter, the present invention will be described in more detail through specific examples or examples, including the accompanying drawings. However, the following specific examples or examples are only one reference for explaining the present invention in detail, and the present invention is not limited thereto, and may be implemented in various forms.

Also, unless defined otherwise, all technical and scientific terms have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terms used in the description of the present invention are only for effectively describing a specific embodiment and are not intended to limit the present invention.

Also, the singular form used in the specification and the appended claims may be intended to include the plural form unless otherwise indicated in the context.

One aspect of the invention relates to a process for producing carbon monoxide by chemical looping combustion, a method of manufacturing the carbon monoxide are a) the MFe _x O _y is reacted with hydrogen in the step of reducing the MFe _x O _y; And b) reacting the reduced MFe _x O _y with carbon dioxide to produce carbon monoxide.

The method for producing carbon monoxide according to the present invention uses MFe _x O _y as an oxygen transfer particle used for chemical roofing combustion, and a chemical roofing combustion technology for producing high-purity carbon monoxide through oxidation and reduction reaction of the MFe _x O _y . It is characterized by providing.

More specifically, as a method for producing carbon monoxide according to the present invention, MFe _x O _y is reacted with hydrogen in a reduction reactor to produce reduced MFe _x O _y , and water is generated as a by-product. Subsequently, as the reduced MFe _x O _y reacts with carbon dioxide in an oxidation reactor, the reduced MFe _x O _y is oxidized again, and carbon monoxide is generated.

Conventional chemical roofing combustion technology provides a method for selectively separating carbon dioxide using fuels such as oxygen and methane and gas containing methane, but the chemical roofing combustion technology of the present invention uses the MFe _x O _y repeatedly. It provides a method of converting carbon dioxide, the main source of greenhouse gas, into carbon monoxide.

In the oxygen transfer particle MFe _x O _y according to the present invention, the M is a metal particle, any one selected from Mn, Ni, Cu, Zn, Cr, Co, Ba, Ca, Sr, Be and Mg or mixtures thereof to be.

In addition, x is an integer of 1 to 10, preferably 1 to 8, more preferably 1 to 5, and y is an integer of 2 to 20, preferably 2 to 15, and more preferably 2 to 10.

MFe _x O _y satisfying the above range can supply sufficient oxygen to hydrogen, as it has a high oxygen transfer capacity.

The oxygen transfer particle MFe _x O _y may be prepared by a known method for producing ferrite particles, and specifically, for example, by adding an iron precursor to a solution in which MO particles are dispersed, and reacting at a high temperature. Can be.

The material that can be used as the iron precursor can be used without limitation as long as it can react with MO to form ferrite particles.

More specifically, for example, iron oleate (Fe (C ₁₇ H ₃₃ COO) ₃ ), iron carboxylate (Fe (COO) ₃ ), iron acetate (Fe (CH ₃ COO) ₂ ), iron nitrate (Fe (NO ₃ ) ₃ ), iron hydroxide (Fe (OH) ₂ ), iron carbonate (FeCO ₃ ), iron oxide (Fe ₂ O ₃ ), or the like, or a mixture thereof, and the amount of iron precursor added is MO The solution may be 50 to 200% by weight, preferably 70 to 180% by weight, and more preferably 80 to 160% by weight, but is not limited thereto.

In addition, the conditions for reacting the MO and the iron precursor may be to fire at 0.5 to 12 hours at 50 to 1,500 ° C, preferably at 1 to 10 hours at 150 to 1,500 ° C, and more preferably at 2 to 6 hours at 200 to 1,500 ° C. However, it is not limited to the reaction conditions.

In one aspect of the present invention, the MFe _x O _y may be characterized by being MgFe ₂ O ₄ , but is not limited thereto.

Although not limited as a method for producing the MgFe ₂ O ₄ , for example, MgO and Fe ₂ O ₃ particles may be prepared by dispersing particles in a solvent, removing the solvent through a known drying method, and reacting at a high temperature. However, it is not limited thereto.

More specifically, after dispersing MgO and Fe ₂ O ₃ particles in a solvent, 0.5 to 12 hours at 300 to 1,500 ° C., preferably 1 to 10 hours at 500 to 1,500 ° C., more preferably 2 to 800 to 1,500 ° C. It may be to react for 6 hours to prepare MgFe ₂ O ₄ , but is not limited to the above method.

The solvent is not limited as long as it can disperse MgO and Fe ₂ O ₃ particles, and specifically, for example, it may be to use any one or a mixture thereof selected from distilled water and ethanol.

Further, the manufacturing method may further include a process such as ball-milling to further improve the dispersibility of MgO and Fe ₂ O ₃ .

MgFe ₂ O ₄ prepared by the above manufacturing method may exhibit a spinel structure of AB ₂ O ₄ , and as there are many oxygen vacancy, electrons of each of A and B ions are easily transferred, so that There is an advantage of excellent redox reactivity.

In addition, the particle size of the MgFe ₂ O ₄ may be 1 to 500 μm, preferably 10 to 400 μm, and more preferably 20 to 300 μm, but is not limited thereto.

When the MgFe ₂ O ₄ is used as the oxygen transport particles, the conversion rate of carbon dioxide, which is reduced to carbon monoxide, is improved, and accordingly, the selectivity of carbon monoxide is increased. Specifically, as the MgFe ₂ O ₄ reduced through the step a) is easily oxidized to MgFe ₂ O ₄ by reacting with the carbon dioxide introduced in the step b), the effect of reducing the carbon dioxide to carbon monoxide is excellent.

In addition, as MgFe ₂ O ₄ contains magnesium (Mg) as a metal particle, it is inexpensive compared to the high cost of nickel (Ni), cerium (Ce), and zirconium (Zr) as a metal in a conventional oxygen transfer particle. , It has the advantage of producing high value-added carbon monoxide without causing an increase in manufacturing cost.

Thus, when carbon monoxide is produced by the manufacturing method according to the present invention, not only is the price of the oxygen-transfer particles used in the oxidation-reduction reaction cheap, but also hydrogen and carbon dioxide, which are fuel gases input in steps a) and b), are also highly purified. Even if it is used as a low-cost, it is low in cost, whereas the carbon monoxide produced has a high price and is very economical.

Subsequently, looking at the steps a) and b) according to the present invention in more detail, the step a) is a step of reducing the MFe _x O _y oxygen transport particles, and the reaction of producing water using hydrogen as a reducing agent proceeds. And MFe _x O _y is converted to reduced MFe _x O _y .

Thereafter, step b) is a step of oxidizing the reduced MFe _x O _y again, converting the reduced MFe _x O _y to MFe _x O _y using carbon dioxide as an oxidizing agent, and a reaction for producing carbon monoxide proceeds.

In one aspect of the present invention, steps a) and b) may be repeated sequentially, but are not limited thereto.

Specifically, as the MFe _x O _y reduction reaction in step a) and the oxidation reaction in step b) are sequentially repeated, high-purity carbon monoxide may be prepared as a final product.

In addition, the reaction by chemical roofing combustion can be maintained through the repeated oxidation-reduction reaction of the MFe _x O _y , and the selectivity of the final product, carbon monoxide, is increased.

In one aspect of the present invention, MFe _x O _y reduced in step b) may be oxidized and regenerated as oxygen transfer particles, but is not limited thereto.

Specifically, in step b), the reduced MFe _x O _y may be regenerated as MFe _x O _y through a reaction in which oxidant carbon dioxide is converted to carbon monoxide, and regenerated MFe _x O _y may be reused to regenerate a) and b) This has the effect of repeating the steps.

In one aspect of the present invention, the method for producing the carbon monoxide may be performed using a fixed bed reactor or a fluidized bed reactor, but is not limited thereto.

The method for producing carbon monoxide using the fixed bed reactor is a general process form of conventional chemical roofing combustion, in which a) and b) steps are sequentially performed in a single reactor, or each step in a reactor in which oxidation and reduction reactors are connected in parallel. It can be done.

For a specific example, steps a) and b) are sequentially performed in a reactor in which MFe _x O _y is input, and at this time, nitrogen, argon, and helium are selected to exchange internal gases before and after each a) and b) step. The purge process can be performed by any one or a mixed inert gas.

In addition, when two fixed bed reactors are used, as shown in FIG. 1, hydrogen is injected into the first reactor to react with MFe _x O _{y in} step a, and carbon dioxide is injected into the second reactor to reduce b). It may be to react the MFe _x O _y , wherein the hydrogen and carbon dioxide may be alternately injected into each reactor to prepare carbon monoxide, but is not limited thereto.

In addition, the method for producing carbon monoxide using a fluidized bed reactor may further include transferring the recycled MFe _x O _y after step b) for reuse in step a).

Further, each reactor may include a gas inlet and a gas outlet.

The gas inlet may be located at the bottom of each reactor, and gas fuel is injected through the inlet. The flow rate of the gas to be injected can be arbitrarily adjusted by a person skilled in the art, and a dispersion plate or the like can be installed at the gas inlet to improve the dispersibility of the gas.

More specifically, using the reactor according to the present invention, for example, after performing the step a) by injecting hydrogen through the gas inlet of the reduction reactor, the inside of the reactor is converted into a nitrogen atmosphere, Carbon dioxide may be injected to perform step b), and b) MFe _x O _y regenerated after the step moves to an oxidation reactor through a transfer tube to participate in an oxidation reaction, and the oxidation-reduction reaction according to the present invention is repeatedly performed Can be.

In addition, the reactor may further include a condensation and separation device for removing water generated through the reaction of step a).

The moving tube may be any form known in the art as long as it can transport MFe _x O _y particles, and specific examples include, for example, solid circulation and gas leakage prevention, loopseal for maintaining pressure balance, Seal pots, J valves, L valves, and U valves may be used, but are not limited thereto.

Gas and carbon monoxide that have not participated in the reaction may be discharged from the gas outlet of each reactor. After all, the manufacturing method according to the present invention can discharge hydrogen, carbon dioxide and carbon monoxide through an outlet, and the hydrogen and carbon dioxide can be separated and collected and reused as gas fuels in steps a) and b).

This solves the problem of generating nitrogen oxides, which are air pollutants, as the conventional chemical roofing combustion reaction uses air as an oxidizing agent, and has the advantage of preventing environmental pollution by consuming carbon dioxide that causes a greenhouse effect as fuel.

In one aspect of the present invention, after the step b) may further include a carbon monoxide separation step, but is not limited thereto.

Specifically, the step b) is a step of injecting carbon dioxide to generate carbon monoxide, which is a mixture of carbon dioxide and carbon monoxide that have not participated in the reaction.

Accordingly, in order to selectively separate carbon monoxide from the mixed gas, the method may further include separating carbon monoxide through a known carbon monoxide condensation method.

Although not limited to the above condensation method, for example, it may be to separate carbon monoxide from a mixed gas using a known adsorbent such as silica and alumina.

Through this, high-purity carbon monoxide can be recovered, and unreacted carbon dioxide in the reactor can be used again in step a) to repeatedly perform a carbon monoxide production reaction by chemical roofing combustion.

In one aspect of the present invention, the steps a) and b) may be performed independently of each other at a temperature range of 500 to 1,500 ° C, preferably 600 to 1,200 ° C, and more preferably 700 to 1,000 ° C, but are not limited thereto. It is not.

Step a) and b) according to the present invention is a step of performing a reduction and oxidation reaction of MFe _x O _y , which is an oxygen transfer particle, and is preferable because the reaction of each step can be easily performed in the above temperature range.

Specifically, as step a) is performed in the temperature range, the oxygen transfer ability of MFe _x O _y is maximized, and it can be quickly reduced after supplying sufficient oxygen to hydrogen.

In addition, as step b) is performed in the temperature range, the reduced MFe _x O _y is readily oxidized by reacting with carbon dioxide, and thus has the advantage of producing carbon monoxide with excellent carbon monoxide selectivity.

That is, by performing steps a) and b) in the above temperature range, the oxygen transfer capacity of MFe _x O _y is improved, it has an excellent carbon dioxide conversion rate, and the selectivity of carbon monoxide is high, thereby maximizing the production of carbon monoxide.

The carbon dioxide conversion rate is a percentage of the number of moles of carbon dioxide reacted in the injected carbon dioxide, and means the carbon dioxide reacted with the reduced MFe _x O _y among the injected carbon dioxide in step b), thereby in step b) according to the present invention. It can be seen how much the reduced MFe _x O _y reacted with carbon dioxide.

Specifically, the number of moles of injected carbon dioxide may be calculated from the concentration of injected carbon dioxide, and the number of moles of reacted carbon dioxide may be calculated using the concentration of carbon monoxide discharged.

In one embodiment of the present invention, the method for producing the carbon monoxide may have a maximum conversion rate of carbon dioxide of 70% or more, preferably 72% or more, and more preferably 75% or more, but is not limited thereto.

The method for producing carbon monoxide according to the present invention has excellent conversion characteristics of carbon dioxide to carbon monoxide by reducing MFe _x O _y , which is an oxygen transfer particle, and has a high conversion rate in the above range.

Accordingly, it is possible to convert carbon monoxide from the injected carbon dioxide at a high rate, thereby having excellent carbon monoxide selectivity.

The carbon monoxide selectivity is a percentage of carbon monoxide in the total gas discharged through the outlet of the reactor, and the higher the selectivity of carbon monoxide, the better the process efficiency.

In one embodiment of the present invention, the method for producing the carbon monoxide may be a maximum selectivity of carbon monoxide of 70% or more, preferably 72% or more, more preferably 75% or more.

The method for producing carbon monoxide according to the present invention has the advantage of having excellent process efficiency and minimizing the separation process of gases as it has a high carbon monoxide selectivity in the above range.

That is, the method for producing carbon monoxide according to the present invention is excellent in efficiency of converting carbon dioxide injected into carbon monoxide through repetition of the oxidation-reduction reaction of MFe _x O _y , thereby obtaining carbon monoxide with high selectivity and high purity carbon monoxide. Mass production of is possible.

In addition, high-purity carbon monoxide can be produced at low cost by using carbon dioxide, a greenhouse gas, as a raw material, thereby reducing the amount of carbon dioxide emitted in industry and providing carbon monoxide having high added value.

In addition, the method for producing carbon monoxide according to the present invention does not generate harmful substances in the reaction process, and it is possible to miniaturize equipment by producing carbon monoxide only with a reactor, and has excellent process efficiency.

Hereinafter, the present invention will be described in more detail based on Examples and Comparative Examples. However, the following examples and comparative examples are only examples for explaining the present invention in more detail, and the present invention is not limited by the following examples and comparative examples.

[Production Example 1]

MgO 2 (Alfa Aesar) 40.304 g, Fe ₂ O ₃ (Alfa Aesar) 159.69 g and 300 mL of ethanol were mixed and ball-milled for 24 hours, and calcined at 1,200 ° C. for 3 hours to prepare MgFe ₂ O ₄ .

The prepared MgFe ₂ O ₄ was analyzed by X-Ray Diffraction (XRD) pattern using MAX-2500 (RIGAKU). As shown in FIG. 2, after reduction to H ₂ , Mg _1-x Fe _x O and Fe It was observed that the crystal structure was changed by oxidation with CO ₂ and then the crystal structure was changed by MgFe ₂ O ₄ and Mg _1-x Fe _x O.

In addition, as a result of measuring MgFe ₂ O ₄ prepared at an accelerated voltage of 10.0 kV using SU8230 (Hitachi) FE-SEM equipment, it was confirmed that it has a particle size of 50 to 150 μm as shown in FIG. 3.

[Example 1]

After 10 g of MgFe ₂ O ₄ prepared in Preparation Example 1 was charged to the reactor, the temperature was increased from room temperature to 900 ° C. while flowing argon gas. After an isothermal condition in which the reactor was maintained at 900 ° C was formed, hydrogen was injected at 200 ml / min to completely reduce MgFe ₂ O ₄ for 1 hour. Thereafter, argon gas was flowed at 200 ml / min to make the reactor inert atmosphere, and then 5% by volume of CO ₂ / Ar was flowed at 200 ml / min to discharge the exhaust gas using YL6100 GC (Gas Chromatography, Younglin). It was measured. At this time, 60/80 CARBOXEN 1000 (SUPELCO, # 21377) was used for the packed bed column, and argon was used as a carrier gas to measure the flow rate at 30 ml / min. In addition, the detector was measured at 40 ℃ isothermal condition using a thermal conductivity detector (Thermal Conductivity Detector, TCD). The completion of the reaction was based on when the generation of carbon monoxide, a product, was not detected through a gas analyzer. The gas analysis results of MgFe ₂ O ₄ including the selectivity of carbon monoxide are shown in FIG. 4.

The amount of carbon monoxide produced from Example 1 was 97.31 L / kg, and the maximum carbon dioxide conversion rate and carbon monoxide selectivity were 75%. In addition, it was confirmed that the maximum conversion rate and selectivity were maintained for 80 minutes.

[Example 2]

It was carried out in the same manner as in Example 1, except that MgFe ₂ O ₄ in Example 1 was changed to CuFe ₂ O ₃ . The gas analysis results of CuFe ₂ O ₃ including the selectivity of carbon monoxide are shown in FIG. 5.

The amount of carbon monoxide produced from Example 2 was 54.08 L / kg, and the maximum carbon dioxide conversion rate and carbon monoxide selectivity were 70%. In addition, it was confirmed that the maximum conversion rate and selectivity were maintained for 5 minutes.

[Comparative Example 1]

It was carried out in the same manner as in Example 1, except that in Example 1 MgFe ₂ O ₄ was changed to Fe ₂ O ₃ .

It was confirmed that the carbon monoxide produced from Comparative Example 1 had a very small production amount and a very low carbon dioxide conversion rate and carbon monoxide selectivity.

Claims (9)

a) is reacted with a MFe _x O _y hydrogen reduction step of the MFe _x O _y; And
b) preparing carbon monoxide by reacting the reduced MFe _x O _y with carbon dioxide;
A method of manufacturing carbon monoxide by chemical roofing, comprising:
(M is Mn, Ni, Cu, Zn, Cr, Co, Ba, Ca, Sr, Be and any one selected from Mg or a mixture thereof;
X is an integer from 1 to 10;
Y is an integer from 2 to 20.) According to claim 1,
The MFe _x O _y is a method for producing carbon monoxide, characterized in that MgFe ₂ O ₄ . According to claim 1,
The steps a) and b) is a method for producing carbon monoxide that is repeated sequentially. According to claim 1,
The method of producing carbon monoxide, wherein the reduced MFe _x O _y in step b) is oxidized and regenerated as oxygen transfer particles. According to claim 1,
The method for producing the carbon monoxide is performed using a fixed bed reactor or a fluidized bed reactor. According to claim 1,
Method of producing a carbon monoxide further comprising the step of separating the carbon monoxide after the step b). According to claim 1,
The steps a) and b) independently of each other is a method for producing carbon monoxide, which is performed in a temperature range of 500 to 1,500 ° C. According to claim 1,
A method for producing carbon monoxide having a maximum conversion rate of carbon dioxide of 70% or more. According to claim 1,
Method for producing carbon monoxide having a maximum selectivity of the carbon monoxide of 70% or more.

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