KR102118318B1 - Integrated multi-stage reactor for methanation of carbon oxides - Google Patents

Abstract

The present invention relates to an integral multi-stage reactor for the methanation of carbon oxide, and more specifically, in a reactor for methanation by reacting carbon monoxide or carbon dioxide with hydrogen, the body formed in a hollow tubular shape so that gas flows therein The first chamber is disposed at the bottom of the inside of the main body, and is provided at a lower end of the first chamber, and is provided at the bottom of the main body, so that a high temperature catalytic conversion reaction occurs with a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen. A first gas distributor which is disposed between a supply unit provided to supply a mixed gas, the supply unit and the lower end of the first chamber, and is provided to uniformly distribute carbon monoxide or carbon dioxide and hydrogen supplied from the supply unit to the first chamber, The first heat exchanger is connected to the upper portion of the first chamber, and is provided to lower the temperature of the mixed gas flowed from the first chamber through heat exchange through a refrigerant. A second gas provided with a catalyst comprising a carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber to cause a catalytic conversion reaction with the catalyst is disposed between the first heat exchanger and the bottom of the second chamber, and A second gas distributor provided to uniformly distribute the carbon, water, carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber to the second chamber, connected to the top of the second chamber, and mixed from the second chamber A second heat exchanger provided to lower the temperature of the gas by performing heat exchange through a refrigerant, disposed on top of the second heat exchanger, and a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen flowed from the second chamber and the catalyst A third chamber provided to cause a catalytic conversion reaction together, disposed between the second heat exchanger and the lower end of the third chamber, removes carbon, water, carbon monoxide or carbon dioxide and hydrogen flowed from the second chamber. A third gas distributor provided to distribute evenly to the three chambers, the phase of the third chamber A third heat exchanger that is connected to a portion and is provided to lower the temperature of the mixed gas flowed from the third chamber by performing heat exchange through a refrigerant, is provided on the top of the main body, and is disposed on the top of the third heat exchanger. , And a discharge portion through which methane and water generated by the reaction of carbon monoxide or carbon dioxide with hydrogen and a catalyst are discharged.

Description

INTEGRATED MULTI-STAGE REACTOR FOR METHANATION OF CARBON OXIDES}

The present invention relates to a reactor for the methanation of carbon oxide, and more specifically, to improve the heat exchange efficiency by integrally forming a reactor that produces methane by reacting carbon oxides such as carbon monoxide or carbon dioxide with hydrogen in multiple stages. It relates to an integral multistage reactor for the methanation of carbon.

Methane is used as a very important energy resource in industrial sites, catering and fuel, and transportation. Methane-based infrastructure is widely distributed worldwide, and it has a very important position in the modern industry.

Most of the methane currently used comes from natural gas based on fossil fuels. In order to respond to problems such as finite nature of fossil fuels and climate change, discussions on how to supply methane in a sustainable manner are actively conducted. In particular, many studies have been conducted on a method for producing methane from carbon monoxide containing carbon monoxide or carbon dioxide generated when methane is burned.

Methane production can be divided into a low temperature reaction of 70° C. or lower in a mixed tank reactor and a reaction of 250° C. or higher in a fixed bed reactor using a catalyst. Low-temperature reactions have low reaction yields and low reaction rates, and research on fixed-bed reactors using catalysts is mainly conducted. The methanation reaction using a catalyst can be divided into a reaction using carbon monoxide and a reaction using carbon dioxide, and each reaction formula is as follows.

CO + 3H ₂ ↔ CH ₄ + H ₂ O(g) -206kJ/mol (at 298K)

CO ₂ + 4H ₂ ↔ CH ₄ + 2H ₂ O(g) -164kJ/mol (at 298K)

All of the above reactions are exothermic reactions, and water is commonly produced. When the reaction is carried out using a catalyst, it is often carried out at a high temperature of 400°C to 500°C, and the reaction proceeds rapidly, but there is a problem that the conversion rate is lowered due to the generated reaction heat.

In addition, in the case of a plurality of reactors, complicated equipment including a plurality of heat exchangers and gas recirculation parts is required to prevent overheating of the reactor, and accordingly, a problem in that the volume of the reactor becomes larger than necessary occurs.

Publication Patent Publication No. 10-2007-0015564 (2007.02.05.)

The technical problem to be achieved by the present invention is to integrate carbon monoxide or carbon dioxide such as carbon dioxide by reacting with hydrogen to form a reactor to produce methane in multiple stages to effectively remove reaction heat generated during the methanation process, thereby improving heat exchange efficiency. It is to provide an integrated multi-stage reactor for the methanation of carbon oxides.

The technical problem to be achieved by the present invention is not limited to the technical problems mentioned above, and other technical problems not mentioned can be clearly understood by those skilled in the art from the following description. There will be.

In order to achieve the above technical problem, the integral multi-stage reactor for the methanation of carbon oxide according to the present invention is a reactor for methanation by reacting carbon monoxide or carbon dioxide with hydrogen, in a hollow tubular form so that gas flows therein The formed body portion, the first chamber is disposed at the bottom of the interior of the body portion, and is provided with a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen to a high temperature catalytic conversion reaction, provided at the bottom of the body portion, the first chamber A first gas disposed between the supply unit provided to supply the mixed gas to the bottom, the supply unit and the bottom of the first chamber, and provided to uniformly distribute carbon monoxide or carbon dioxide and hydrogen supplied from the supply unit to the first chamber A distributor, a first heat exchanger connected to the upper portion of the first chamber, and provided to lower the temperature of the mixed gas flowing from the first chamber by performing heat exchange through a refrigerant, disposed on the top of the first heat exchanger , A second chamber provided to cause a catalytic conversion reaction with a catalyst is a carbon monoxide or a mixed gas composed of carbon dioxide and hydrogen flowing from the first chamber, disposed between the first heat exchanger and the lower end of the second chamber , A second gas distributor provided to uniformly distribute carbon, water, carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber to the second chamber, connected to an upper portion of the second chamber, and flowing from the second chamber A second heat exchanger, which is arranged to lower the temperature of the mixed gas by performing heat exchange through a refrigerant, is disposed on top of the second heat exchanger, and a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen flowed from the second chamber A third chamber provided to cause a catalytic conversion reaction together with a catalyst, disposed between the second heat exchanger and the lower end of the third chamber, the carbon, water, carbon monoxide or carbon dioxide and hydrogen flowed from the second chamber A third gas distributor provided to uniformly distribute the third chamber, the third The third heat exchanger is connected to the upper part of the third chamber, and is provided to lower the temperature of the mixed gas flowed from the third chamber by performing heat exchange through the refrigerant. It is disposed in the carbon monoxide or carbon dioxide and methane and water generated by the reaction of hydrogen and the catalyst to provide a discharge portion.

In an embodiment of the present invention, the first heat exchanger is arranged in a coiled long tube to lower the temperature of the mixed gas and catalyst flowed from the first chamber, and the refrigerant flows into one end so that the refrigerant flows therein. It is also possible that the first inlet is provided, the heat exchange is performed at the other end and the first outlet is provided so that the refrigerant is discharged.

In an embodiment of the present invention, the second heat exchanger is disposed in a coiled long tube to lower the temperature of the mixed gas flowed from the second chamber, and from the first outlet at one end so that refrigerant flows therein. It is also possible that a second inlet through which a refrigerant is introduced is provided, and a second outlet is provided so that heat exchange is performed at the other end and the refrigerant is discharged.

In an embodiment of the present invention, the third heat exchanger is arranged in a coiled long tube to lower the temperature of the mixed gas flowed from the third chamber, and from the second outlet at one end so that refrigerant flows therein. A third inlet through which the refrigerant is introduced may be provided, and a third outlet may be provided so that heat exchange is performed at the other end and the refrigerant is discharged.

In an embodiment of the present invention, the first chamber is a mixture gas and a catalyst conversion reaction occurs at a temperature of 400 ℃ to 500 ℃, it is also possible that the mixed gas is primarily cooled in the first heat exchanger.

In an embodiment of the present invention, in the second chamber, the mixed gas cooled by the first heat exchanger and the catalyst undergo a conversion reaction at a temperature of 350°C to 400°C, and the mixed gas is secondary in the second heat exchanger It is also possible to cool.

In an embodiment of the present invention, in the third chamber, the mixed gas cooled by the second heat exchange device undergoes a conversion reaction with a catalyst at a temperature of 250° C. to 350° C., and the mixed gas in the third heat exchange device It is also possible to cool thirdly.

In an embodiment of the present invention, the mixed gas passing through the first chamber, the second chamber, and the third chamber is sequentially cooled by the first heat exchanger, the second heat exchanger, and the third heat exchanger to gradually increase the temperature. It is also possible to lower.

In an embodiment of the present invention, the refrigerant flows sequentially from the second heat exchanger and the first heat exchanger, starting with the third heat exchanger, and is sequentially heated by the third chamber, the second chamber, and the first chamber. It is also possible that the temperature gradually increases.

In an embodiment of the present invention, the hydrogen may be supplied by separating and supplying oxygen and hydrogen through water electrolysis with surplus electricity produced through renewable energy.

In an embodiment of the present invention, the carbon monoxide or carbon dioxide may be to collect and supply carbon monoxide or carbon dioxide discharged through greenhouse gas.

In an embodiment of the present invention, the first heat exchanger may cool the first chamber to produce steam by heating the water produced through the reaction of carbon monoxide or carbon dioxide and hydrogen.

In an embodiment of the present invention, the integral multi-stage reactor for the methanation of carbon oxide may be a methanation process to which the integral multi-stage reactor applied to the methanation process is applied to produce methane produced through the reaction of carbon dioxide and hydrogen.

According to an embodiment of the present invention, carbon dioxide, such as carbon monoxide or carbon dioxide, is reacted with hydrogen to form a reactor that produces methane in multiple stages, thereby effectively removing reaction heat generated during the methanation process, thereby improving heat exchange efficiency. There is an effect that can be made.

It should be understood that the effects of the present invention are not limited to the above-described effects, and include all effects that can be deduced from the configuration of the invention described in the detailed description or claims of the present invention.

1 is a cross-sectional view of an integrated multi-stage reactor for the methanation of carbon oxide according to an embodiment of the present invention.
2 is a schematic diagram of a methanation process to which an integral multi-stage reactor for the methanation of carbon oxide according to an embodiment of the present invention is applied.

Hereinafter, the present invention will be described with reference to the accompanying drawings. However, the present invention may be implemented in various different forms, and thus is not limited to the embodiments described herein. In addition, in order to clearly describe the present invention in the drawings, parts irrelevant to the description are omitted, and like reference numerals are assigned to similar parts throughout the specification.

Throughout the specification, when a part is "connected (connected, contacted, coupled)" with another part, it is not only "directly connected", but also "indirectly connected" with another member in between. "It also includes the case where it is. Also, when a part “includes” a certain component, this means that other components may be further provided instead of excluding other components, unless otherwise stated.

The terms used herein are only used to describe specific embodiments, and are not intended to limit the present invention. Singular expressions include plural expressions unless the context clearly indicates otherwise. In this specification, terms such as “include” or “have” are intended to indicate that a feature, number, step, operation, component, part, or combination thereof described in the specification exists, and that one or more other features are present. It should be understood that the existence or addition possibilities of fields or numbers, steps, operations, components, parts or combinations thereof are not excluded in advance.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings.

1 is a cross-sectional view of an integral multi-stage reactor for methanation of carbon oxide according to an embodiment of the present invention, and FIG. 2 is a methanation to which an integral multi-stage reactor for methanation of carbon oxide according to an embodiment of the present invention is applied It is a process diagram.

1 to 2, the integral multi-stage reactor 100 for the methanation of carbon oxides according to the present invention is a reactor for methanization by reacting carbon monoxide or carbon dioxide with hydrogen, and hollow gas is flowed therein The body portion 110 formed in a tubular shape of the first chamber 121 is disposed at the bottom of the interior of the body portion 110 and is provided so that a high temperature catalytic conversion reaction with a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen occurs ), is provided at the bottom of the main body 110, the supply unit 131 provided to supply the mixed gas to the bottom of the first chamber 121, the supply unit 131 and the bottom of the first chamber 121 The first gas distributor 141, which is disposed between, and is provided to uniformly distribute carbon monoxide or carbon dioxide and hydrogen supplied from the supply unit 131 to the first chamber 121, the upper portion of the first chamber 121 And a first heat exchanger 151 provided to lower the temperature of the mixed gas flowed from the first chamber 121 by performing heat exchange through a refrigerant, and disposed on top of the first heat exchanger 151 The second chamber 122, the first heat exchanger 151, and the second chamber 122 are provided so that a catalytic conversion reaction occurs with a catalyst in which a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber 121 occurs. It is disposed between the lower end of the second chamber 122, the second provided to uniformly distribute the carbon, water, carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber 121 to the second chamber (122) Gas distributor 142, a second heat exchanger connected to the upper portion of the second chamber 122, and provided to lower the temperature of the mixed gas flowing from the second chamber 122 by performing heat exchange through a refrigerant ( 161), disposed on the upper end of the second heat exchanger 161, the mixed gas composed of carbon monoxide or carbon dioxide and hydrogen flowed from the second chamber 122 is configured to cause a catalytic conversion reaction with the catalyst Carbon, water, carbon monoxide or carbon dioxide that is disposed between the empty third chamber 123, the second heat exchanger 161 and the lower end of the third chamber 123, and flows from the second chamber 122, and The third gas distributor 143, which is provided to uniformly distribute hydrogen to the third chamber 123, is connected to the upper portion of the third chamber 123, and the mixed gas flowed from the third chamber 123. A third heat exchanger 171 is provided to lower the temperature by performing heat exchange through a refrigerant, and is provided at the top of the main body 110 and is disposed on the top of the third heat exchanger 171, with carbon monoxide or carbon dioxide. A discharge unit 132 through which methane and water generated by the reaction of hydrogen and a catalyst are discharged is provided.

In an embodiment of the present invention, it includes a body portion 110 formed in a hollow tubular shape so that the gas flows therein.

More specifically, the body portion 110 is formed in a hollow long tubular shape such that carbon oxide and hydrogen such as carbon monoxide or carbon dioxide flow therein. Therefore, carbon oxide and hydrogen flow inside the body portion 110 and react to produce methane.

In addition, the first chamber 121 is provided to be disposed at the bottom of the interior of the body portion 110, and a high temperature catalytic conversion reaction with a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen.

More specifically, the first chamber 121 is disposed at the bottom of the inside of the main body 110, and is supplied with carbon monoxide or carbon dioxide and hydrogen from the outside to produce methane through a high temperature catalytic conversion reaction.

At this time, the catalytic conversion reaction occurs at a high temperature, where the internal flow is a fast fluidized bed region, and the catalyst is generally a nickel-based catalyst, but promotes the reaction of the carbon oxide and hydrogen to methane. If you can produce it is not greatly limited.

In addition, it is provided at the bottom of the main body 110, the supply unit 131 is provided to supply a mixed gas to the bottom of the first chamber (121).

More specifically, the supply unit 131 is provided at the bottom of the main body 110 to supply a mixed gas composed of carbon oxide and hydrogen supplied from the outside to the first chamber (121). Therefore, the supply part 131 may be connected to the main body part 110 by means such as a pipe and supplied to the first chamber 121.

In addition, it is disposed between the lower end of the supply unit 131 and the first chamber 121, the first gas to uniformly distribute the carbon monoxide or carbon dioxide and hydrogen supplied from the supply unit 131 to the first chamber 121 Dispenser 141 is provided.

More specifically, the first gas distributor 141 is disposed between the supply unit 131 and the lower end of the first chamber 121 inside the main body 110 and supplied from the supply unit 131. It is provided to uniformly distribute the mixed gas to the first chamber (121). Accordingly, the first gas distributor 141 uniformly distributes the mixed gas to effectively effect a catalytic conversion reaction.

In addition, it is connected to the upper portion of the first chamber 121, the first heat exchanger 151 is provided to lower the temperature of the mixed gas flowed from the first chamber 121 by performing heat exchange through a refrigerant.

More specifically, the first heat exchanger 151 is connected to the upper portion of the first chamber 121 inside the main body 110 to cool the mixed gas and flows from the first chamber 121 The temperature of the mixed gas is cooled by heat exchange through a refrigerant.

At this time, the refrigerant is not greatly limited as long as it can cool the mixed gas, but is preferably water. Therefore, it is also possible to re-inject water from the methane and water produced through the methanation process as a refrigerant.

In addition, the second chamber 122 is disposed on the upper end of the first heat exchanger 151, the mixed gas composed of carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber 121 to the catalytic conversion reaction with the catalyst ) Is provided.

In more detail, the second chamber 122 is disposed on the top of the first heat exchanger 151 inside the main body 110, and carbon monoxide cooled through the first heat exchanger 151 or Methane is produced through a catalytic conversion reaction with a catalyst composed of carbon dioxide and hydrogen.

That is, in the second chamber 122, a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber 121 is cooled through the first heat exchanger 151, and the catalyst is converted through the catalyst. The reaction takes place.

In addition, carbon, water, carbon monoxide or carbon dioxide and hydrogen flowing from the first heat exchanger 151 and the lower end of the second chamber 122 are flown from the first chamber 121 to the second chamber ( A second gas distributor 142 is provided to uniformly distribute to 122).

More specifically, the second gas distributor 142 is disposed between the first heat exchanger 151 and the lower end of the second chamber 122 in the main body 110. It is provided to uniformly distribute the mixed gas flowing from (151) to the second chamber (122). Therefore, the second gas distributor 142 uniformly distributes the mixed gas to effectively effect a catalytic conversion reaction.

In addition, a second heat exchanger 161 is provided to be connected to the upper portion of the second chamber 122 and to lower the temperature of the mixed gas flowing from the second chamber 122 by performing heat exchange through a refrigerant.

More specifically, the second heat exchanger 161 is connected to the upper portion of the second chamber 122 in the interior of the main body 110 to cool the temperature of the mixed gas, the second chamber 122 The temperature of the mixed gas flowing therefrom is cooled by heat exchange through a refrigerant.

In addition, the third chamber 123 is disposed on the upper end of the second heat exchanger 161, and a catalytic conversion reaction occurs with the catalyst of a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen flowing from the second chamber 122. ) Is provided.

The third chamber 123 is disposed on the top of the second heat exchanger 161 inside the main body 110, and is composed of carbon monoxide or carbon dioxide and hydrogen cooled through the second heat exchanger 161. Methane is produced through a catalytic conversion reaction with a mixed gas catalyst.

In addition, the third chamber is disposed between the second heat exchanger 161 and the lower end of the third chamber 123, and the carbon, water, carbon monoxide or carbon dioxide and hydrogen flowed from the second chamber 122 are disposed in the third chamber ( A third gas distributor 143 is provided to uniformly distribute to 123).

More specifically, the third gas distributor 143 is disposed between the second heat exchanger 161 and the lower end of the third chamber 123 inside the main body 110. It is provided to uniformly distribute the mixed gas flowed from the (161) to the third chamber (123). Therefore, the third gas distributor 143 uniformly distributes the mixed gas to effectively effect a catalytic conversion reaction.

In addition, a third heat exchanger 171 is provided to be connected to the upper portion of the third chamber 123 and to lower the temperature of the mixed gas flowing from the third chamber 123 by performing heat exchange through a refrigerant.

More specifically, the third heat exchanger 171 is connected to the upper portion of the third chamber 123 inside the main body 110 to cool the temperature of the mixed gas, and the third chamber 123 The temperature of the mixed gas flowing therefrom is cooled by heat exchange through a refrigerant.

In addition, it is provided on the top of the main body portion 110 is disposed on the upper portion of the third heat exchanger 171, carbon monoxide or carbon dioxide and methane and water generated by the reaction of hydrogen and the discharge unit 132 is discharged It is provided.

More specifically, the mixed gas composed of carbon monoxide or carbon dioxide and hydrogen introduced through the supply unit 131 provided at the bottom of the main body 110 is provided in the first chamber 121, the second chamber 122, and the third. After passing through the chamber 123, it reacts with the catalyst to produce methane and water, and is discharged through the discharge portion 132 formed on the top of the body portion 110.

At this time, the discharge portion 132 is connected by means such as a pipe and the top of the body portion 110 to discharge methane and water.

In addition, the third heat exchanger 171 is disposed in a coiled long tube to lower the temperature of the mixed gas flowed from the third chamber 123, and the third refrigerant is introduced into one end so that the refrigerant flows therein. An inlet 172 may be provided, and a third outlet 173 may be provided so that heat exchange is performed at the other end and refrigerant is discharged.

In more detail, the third heat exchanger 171 is formed in a coiled elongated tube, and a refrigerant flows therein, and the third heat exchanger 171 is transferred from the third chamber 123 by the refrigerant. The mixed gas flowing to the discharge unit 132 is cooled by heat exchange.

Therefore, a third inlet 172 through which a refrigerant flows from the outside is provided at one end of the third heat exchanger 171, and the refrigerant introduced through the third inlet 172 passes through a tube formed in a coil shape. , Cooling the mixed gas passing outside of the third heat exchanger 171, and after the heat exchange is performed, is discharged through the third outlet 173 of the other end.

In addition, the second heat exchanger 161 is disposed in a coiled long tube to lower the temperature of the mixed gas flowed from the second chamber 122, and the third outlet 173 at one end so that the refrigerant flows therein. ) Is provided with a second inlet 162 through which the refrigerant flows, and a second outlet 163 may be provided so that heat exchange is performed at the other end and the refrigerant is discharged.

In more detail, the second heat exchange device 161 is formed of a coiled elongated tube, and a refrigerant flows therein, and the second heat exchange device 161 is transferred from the second chamber 122 by the refrigerant. The mixed gas flowing into the third chamber 123 is cooled by heat exchange.

Therefore, a second inlet 162 through which a refrigerant flows from the third outlet 173 is provided at one end of the second heat exchanger 161 and connected to the third outlet 173, and the second inlet 162 ) By passing the refrigerant flowing through the tube formed in a coil shape, cools the mixed gas passing through the outside of the second heat exchanger 161, and after the heat exchange is performed, the second outlet 163 provided at the other end The refrigerant is discharged through.

In addition, the first heat exchanger 151 is disposed in a coiled long tube to lower the temperature of the mixed gas flowed from the first chamber 121, and the second outlet 163 at one end so that the refrigerant flows therein. ), a first inlet 152 through which a refrigerant flows is provided, and a first outlet 153 may be provided so that heat exchange is performed at the other end and the refrigerant is discharged.

In more detail, the first heat exchanger 151 is formed in a coiled elongated tube, and a refrigerant flows therein, and the first heat exchanger 151 is transferred from the first chamber 121 by the refrigerant. The mixed gas flowing into the second chamber 122 is cooled by heat exchange.

Therefore, a first inlet 152 through which a refrigerant flows from the second outlet 163 is connected to the second outlet 163 at one end of the first heat exchanger 151, and the first inlet 152 ) By passing the refrigerant flowing through the tube formed in a coil shape, cools the mixed gas passing through the outside of the first heat exchanger 151, and after the heat exchange is performed, the first outlet 153 provided at the other end The refrigerant is discharged through.

In addition, a conversion reaction occurs at a temperature of 400°C to 500°C in the first chamber 121, and the mixed gas may be primarily cooled in the first heat exchanger 151.

In more detail, the first chamber 121 has a catalytic conversion reaction at a high temperature of 400°C to 500°C in order to increase the reaction rate of the mixed gas and catalyst introduced through the supply unit 131, and the heated mixed gas It is primarily cooled by the first heat exchanger 151. Therefore, the first chamber 121 is capable of efficiently producing methane by performing a catalytic conversion reaction at a high temperature.

Further, in the second chamber 122, the mixed gas and the catalyst cooled by the first heat exchanger 151 undergo a conversion reaction at a temperature of 350°C to 400°C, and are mixed in the second heat exchanger 161. The gas and catalyst can be cooled secondarily.

More specifically, in the second chamber 122, the mixed gas and the catalyst introduced through the first chamber 121 undergo a conversion reaction at a temperature of 350°C to 400°C, and the first chamber 121 As the conversion reaction occurs at a low temperature, an equilibrium conversion rate higher than the reaction rate can be achieved, and the heated mixed gas is secondarily cooled by the second heat exchanger 161 to efficiently produce methane.

In addition, in the third chamber 123, the mixed gas cooled by the second heat exchanger 161 and the catalyst undergo a conversion reaction at a temperature of 250°C to 350°C, and the mixed gas in the third heat exchanger 171 Can be cooled thirdly.

More specifically, in the third chamber 123, a mixed gas and a catalyst introduced through the second chamber 122 undergo a conversion reaction at a temperature of 250°C to 350°C, than the second chamber 122. When the conversion reaction occurs at a low temperature, an equilibrium conversion rate higher than the reaction rate can be achieved, and the heated mixed gas is cooled thirdly by the third heat exchanger 171 to efficiently produce methane.

In addition, the mixed gas passing through the first chamber 121, the second chamber 122 and the third chamber 123 is the first heat exchanger 151, the second heat exchanger 161 and the third heat exchanger ( 171) may be sequentially cooled, and the temperature may gradually decrease.

More specifically, the first chamber 121, the second chamber 122 and the third chamber 123 are sequentially disposed inside the main body 110, the first chamber 121 and the first A first heat exchanger 151 is disposed between the two chambers 122, and a second heat exchanger 161 is disposed between the third chambers 123 of the second chamber 122, and the third chamber ( A third heat exchanger 171 is disposed on the upper portion of the 123, and the mixed gas passes sequentially through the first chamber 121, the second chamber 122 and the third chamber 123, and the catalyst is converted together with the catalyst. As the reaction is performed, the mixed gas is sequentially cooled through the first heat exchanger 151, the second heat exchanger 161, and the third heat exchanger 171.

Therefore, it is possible to efficiently produce methane by performing a catalytic conversion reaction at an initial high temperature condition and having a high reaction rate and sequentially carrying out a catalytic conversion reaction at a low temperature to have a high equilibrium conversion rate.

In addition, the refrigerant flows in the order of the second heat exchanger 161 and the first heat exchanger 151, starting with the third heat exchanger 171, so that the third chamber 123, the second chamber 122 and the second The temperature may be gradually increased by being sequentially heated by one chamber 121.

More specifically, the third heat exchanger 171, the second heat exchanger 161, and the first heat exchanger 151 are connected to each other so that the refrigerant flows sequentially, and the refrigerant is the third chamber 123, the third As the two chambers 122 and the first chamber 121 are cooled, the temperature of the refrigerant gradually increases.

That is, the mixed gas is supplied to the bottom relative to the main body and the temperature decreases as it moves to the top, and the temperature increases as the refrigerant moves from the top to the bottom based on the main body 110.

In addition, hydrogen can be supplied by separating oxygen and hydrogen through water electrolysis with surplus electricity produced through renewable energy.

More specifically, the hydrogen is supplied by separating oxygen and hydrogen by electrolysis of water, and can be obtained through renewable energy or surplus electricity produced through a power plant.

For example, in an isolated space such as an island, oxygen and hydrogen are separated by electrolysis of water through surplus energy generated through wind or solar power generation, and the produced oxygen is sold, and carbon oxide is supplied through the rest of the hydrogen. It can be methanized and used as energy.

In addition, carbon monoxide or carbon dioxide can be supplied by collecting carbon monoxide or carbon dioxide emitted through greenhouse gases.

More specifically, the carbon monoxide, such as carbon monoxide or carbon dioxide, can be easily obtained through the use of automobile fumes or fossil fuels, and carbon dioxide can be collected and methaneized.

In addition, the first heat exchanger 151 may cool the first chamber 121 to heat the water generated through the reaction of carbon monoxide or carbon dioxide and hydrogen to produce steam.

More specifically, in the first chamber 121, a conversion reaction of a mixed gas and a catalyst occurs at a temperature of 400°C to 500°C, and the first heat exchanger 151 cools it.

Therefore, since the refrigerant of the first heat exchanger 151 maintains a high temperature, steam can be obtained by heating water through this, and the steam produced through this can be sold or generated to generate electricity.

In addition, the integrated multi-stage reactor 100 for the methanation of carbon monoxide or carbon dioxide can be applied to the methanation process to produce methane produced through the reaction of carbon dioxide and hydrogen.

는 아래의 계산식을 따른다.In addition, in the integrated multi-stage reactor for the methanation of carbon monoxide or carbon dioxide according to the present invention, the catalyst reacts with the mixed gas and the fluidized bed rather than the fixed bed, thereby preventing heat recovery and high heat of the catalyst (reaction heat) at the same time as the reaction. (141), the second gas distributor 142 and the third gas distributor 143, the minimum fluidization rate calculation formula according to the input of the catalyst

Follows the formula below.

= minimum fluidizing condition,

= minimum fluidizing condition,

= screen size

= screen size

= gas density

= gas density

= coefficient of viscosity

= coefficient of viscosity

= bed voidage

= bed voidage

= (

) _{of same volume}

= (

) _{of same volume}

(sheres), 0<

<1(all other particle shapes)

(sheres), 0<

<1(all other particle shapes)

= particle density or catalyst density

= particle density or catalyst density

= gravitational acceleration

= gravitational acceleration

In addition, by controlling the size and density of the catalyst particles injected through the first gas distributor 141, the second gas distributor 142 and the third gas distributor 143, the flow rate and speed of carbon monoxide or carbon dioxide and hydrogen are controlled. Can be controlled.

The above description of the present invention is for illustration only, and a person having ordinary knowledge in the technical field to which the present invention pertains can understand that it can be easily modified into other specific forms without changing the technical spirit or essential features of the present invention. will be. Therefore, it should be understood that the embodiments described above are illustrative in all respects and not restrictive. For example, each component described as a single type may be implemented in a distributed manner, and similarly, components described as distributed may be implemented in a combined form.

The scope of the present invention is indicated by the following claims, and all changes or modifications derived from the meaning and scope of the claims and their equivalent concepts should be interpreted to be included in the scope of the present invention.

100: integral multi-stage reactor for the methanation of carbon monoxide or carbon dioxide
110: main body
121: first chamber
122: second chamber
123: third chamber
131: supply
132: outlet
141: first gas distributor
142: second gas distributor
143: third gas distributor
151: first heat exchanger
152: first inlet
153: first outlet
161: second heat exchanger
162: second inlet
163: second outlet
171: third heat exchanger
172: third inlet
173: third outlet

Claims (13)

In the reactor for reacting carbon monoxide or carbon dioxide and hydrogen to methane,
A body portion formed in a hollow tubular shape so that gas flows therein;
A first chamber disposed at the bottom of the inside of the main body and provided with a high temperature catalytic conversion reaction with carbon monoxide or a mixed gas composed of carbon dioxide and hydrogen;
A supply unit provided at a lower end of the main body and provided to supply a mixed gas to a lower end of the first chamber;
A first gas distributor disposed between the supply section and the lower end of the first chamber and provided to uniformly distribute carbon monoxide or carbon dioxide and hydrogen supplied from the supply section to the first chamber;
A first heat exchanger connected to an upper portion of the first chamber and provided to lower the temperature of the mixed gas flowing from the first chamber by performing heat exchange through a refrigerant;
A second chamber disposed on an upper end of the first heat exchanger, and having a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber to perform a catalytic conversion reaction with a catalyst;
A second gas distributor disposed between the first heat exchanger and the lower end of the second chamber and provided to uniformly distribute carbon, water, carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber to the second chamber. ;
A second heat exchanger connected to the upper portion of the second chamber and provided to lower the temperature of the mixed gas flowing from the second chamber by performing heat exchange through a refrigerant;
A third chamber disposed on the upper end of the second heat exchanger and provided with a catalyst composed of carbon monoxide or carbon dioxide and hydrogen flowed from the second chamber to undergo a catalytic conversion reaction with the catalyst;
A third gas distributor disposed between the second heat exchanger and the bottom of the third chamber and provided to uniformly distribute carbon, water, carbon monoxide or carbon dioxide and hydrogen flowed from the second chamber to the third chamber. ;
A third heat exchanger connected to an upper portion of the third chamber and provided to lower the temperature of the mixed gas flowing from the third chamber by performing heat exchange through a refrigerant;
It is provided on the upper portion of the body portion is disposed on the upper portion of the third heat exchanger, carbon monoxide or carbon dioxide and methane and water generated by the reaction of hydrogen and the discharge portion discharged;
Integral multi-stage reactor for the methanation of carbon monoxide or carbon dioxide comprising a. According to claim 1, The third heat exchanger is arranged in a coil-shaped long tube to lower the temperature of the mixed gas and catalyst flowed from the third chamber, the refrigerant is introduced into one end so that the refrigerant flows inside 3 Inlet multi-stage reactor for the methanation of carbon monoxide or carbon dioxide, characterized in that a third outlet is provided so that the heat exchange is performed at the other end, and the refrigerant is discharged. The method according to claim 2, wherein the second heat exchanger is arranged in a coiled long tube to lower the temperature of the mixed gas flowed from the second chamber, and refrigerant is discharged from the third outlet at one end so that the refrigerant flows therein. An integrated multi-stage reactor for the methanation of carbon monoxide or carbon dioxide, characterized in that a second inlet is introduced, a second outlet is provided so that heat exchange is performed at the other end, and refrigerant is discharged. The method of claim 3, wherein the first heat exchanger is arranged in a coiled long tube to lower the temperature of the mixed gas flowed from the first chamber, and the refrigerant is discharged from the second outlet at one end so that the refrigerant flows therein. Integral multi-stage reactor for methanation of carbon monoxide or carbon dioxide, characterized in that a first inlet is provided, heat exchange is performed at the other end, and a first outlet is provided so that the refrigerant is discharged. The method of claim 4, wherein the first chamber is a mixture of gas and catalyst at a temperature of 400 ℃ to 500 ℃ conversion reaction occurs, the first mixture of carbon monoxide or carbon dioxide, characterized in that the mixed gas is primarily cooled in the heat exchanger Integral multistage reactor for methanation. ◈ Claim 6 was abandoned when payment of the set registration fee was made.◈ According to claim 5, In the second chamber, the mixed gas and the catalyst cooled by the first heat exchanger undergo a conversion reaction at a temperature of 350°C to 400°C, and the mixed gas is secondarily cooled in the second heat exchanger. Integral multi-stage reactor for the methanation of carbon monoxide or carbon dioxide, characterized in that. ◈ Claim 7 was abandoned when payment of the set registration fee was made.◈ The method of claim 6, wherein the third chamber is a mixed gas cooled by the second heat exchanger, a conversion reaction occurs with the catalyst at a temperature of 250°C to 350°C, and the mixed gas is thirdarily generated in the third heat exchanger. Integral multi-stage reactor for the methanation of carbon monoxide or carbon dioxide, characterized by being cooled. ◈ Claim 8 was abandoned when payment of the set registration fee was made.◈ The mixed gas passing through the first chamber, the second chamber and the third chamber is sequentially cooled by the first heat exchanger, the second heat exchanger and the third heat exchanger, and the temperature gradually decreases. Integral multi-stage reactor for the methanation of carbon monoxide or carbon dioxide, characterized in that. The method of claim 1, wherein the refrigerant flows sequentially from the second heat exchanger and the first heat exchanger, starting with the third heat exchanger, and is sequentially heated by the third chamber, the second chamber, and the first chamber to gradually increase the temperature. Integral multi-stage reactor for the methanation of carbon monoxide or carbon dioxide, characterized in that is elevated. According to claim 1, The hydrogen is an integrated multi-stage reactor for the methanation of carbon monoxide or carbon dioxide, characterized in that the supply of oxygen and hydrogen through the electrolysis of surplus electricity produced through renewable energy. According to claim 1, The carbon monoxide or carbon dioxide is an integrated multi-stage reactor for the methanation of carbon monoxide or carbon dioxide, characterized in that by supplying carbon monoxide or carbon dioxide discharged through the greenhouse gas. The method according to claim 1, wherein the first heat exchanger cools the first chamber to heat the water produced through the reaction of carbon monoxide or carbon dioxide and hydrogen to produce steam, thereby producing steam. Integral multi-stage reactor. According to claim 1, The integral multi-stage reactor for the methanation of carbon monoxide or carbon dioxide is applied to the methanation process, characterized in that applied to the methanation process to produce methane produced through the reaction of carbon dioxide and hydrogen.

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