KR102118313B1 - Energy independence system using pure oxygen combustion power generation and new renewable energy - Google Patents

Abstract

The present invention relates to an energy self-reliance system using pure oxygen combustion power generation and renewable energy, and more specifically, a fuel supply unit that supplies low-grade fuel, and thermally decomposes low-grade fuel supplied through the fuel supply unit into an energy source. The low-grade fuel power generation unit, a new and renewable energy unit that produces electricity through new and renewable energy, and a water and electricity dissociation unit that separates hydrogen and oxygen into electricity using the electricity generated through the new and renewable energy unit, and the low-grade fuel power generation. When generating electricity, the pure oxygen supply unit provided to reduce the pollutant emission source by supplying pure oxygen from the faucet dissection or the outside, combines carbon monoxide or carbon dioxide produced through the low-grade fuel generation unit with hydrogen separated through the faucet dissection. It includes a methanation unit to methanize to produce methane and a methane processing unit to collect and store or transport the methane produced through the methanation unit to the outside.

Description

ENERGY INDEPENDENCE SYSTEM USING PURE OXYGEN COMBUSTION POWER GENERATION AND NEW RENEWABLE ENERGY

The present invention relates to an energy self-reliance system, and more specifically, by using pure oxygen combustion power as a base power generation and adding new and renewable energy, it can supply and receive energy itself to improve energy independence. It relates to an energy self-reliance system using renewable energy.

The supply of renewable energy to reduce greenhouse gas is increasing worldwide, and recently Korea also announced a plan to implement “Renewable Energy 2030” aiming to increase the share of domestic renewable energy generation to 20% by 2030.

However, since electricity is difficult to store unlike other energy sources, it must be consumed at the same time as production, but due to the output variability of renewable energy, securing the balance between supply and demand for efficient use of electricity produced by renewable energy sources You need a means for

Therefore, as a means to replace it, research on the methanization of greenhouse gases is currently being actively conducted. Most of these methane are obtained from fossil fuel-based natural gas, and discussions about sustainable methane supply methods are actively conducted in order to simply consume resources to cope with problems such as finite nature of fossil fuels and climate change. 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, although an energy independent island creation project was implemented in Korea to reduce greenhouse gases, the island area that completed this is not enough for energy independence because it relies on measures such as diesel power generation.

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

The technical problem to be achieved by the present invention is to combine methane or hydrogen produced by hydrolysis of carbon monoxide or carbon dioxide generated from pure oxygen combustion power through renewable energy by adding pure renewable energy as base power and adding new renewable energy. Providing an energy self-reliance system using pure oxygen-fired power generation and renewable energy that can improve energy independence by supplying energy by itself.

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 energy independence system using pure oxygen combustion power generation and new and renewable energy according to the present invention thermally decomposes the low-grade fuel supplied through the fuel-supplying unit into an energy source. A low-grade fuel power generation unit that generates electricity, a new and renewable energy unit that generates electricity through new and renewable energy, and a water and electricity dissociation unit that separates hydrogen and oxygen into electricity using the electricity produced through the new and renewable energy unit. When generating power from the fuel generating unit, the pure oxygen supply unit provided to reduce the pollutant emission source by supplying pure oxygen from the water receiving unit or the outside, and the carbon monoxide or carbon dioxide produced through the low-grade fuel generating unit is separated from the hydrogen separated through the water receiving unit. It provides a methanation unit to methanize to combine to produce methane, and a methane processing unit to capture and store or transport the methane produced through the methanation unit to the outside.

In an embodiment of the present invention, the low-grade fuel includes at least one of coal, biomass, and waste, and continuously produces carbon monoxide or carbon dioxide through the low-grade fuel generation unit and supplies it to the methane stably. It is also possible to produce methane.

In an embodiment of the present invention, the renewable energy unit may also generate electricity by using at least one of renewable energy such as wind power, water power, and sunlight.

In an embodiment of the present invention, the methanation unit generates steam by using a large amount of heat generated in the process of producing methane by combining carbon monoxide or carbon dioxide with hydrogen, and generates steam by generating electricity through the steam. The power generation unit may be provided.

In an embodiment of the present invention, the new and renewable energy unit may generate electricity through new and renewable energy, and optionally store it in a battery.

In the embodiment of the present invention, the water electrolysis unit does not supply oxygen and hydrogen separated through the water electrolysis to methane according to the situation, but through fuel cell power generation that generates electricity through the energy of oxidation and reduction reactions. It is also possible that a fuel cell generator for producing electricity is provided.

In an embodiment of the present invention, it is also possible to produce water by supplying water used for the water electrolysis unit to seawater and combining hydrogen separated through the water electrolysis unit with carbon monoxide or carbon dioxide produced through the low-grade fuel power generation unit. Do.

In an embodiment of the present invention, the methanation unit is provided with a reactor such that carbon monoxide or carbon dioxide is synthesized into methane by a catalytic conversion reaction by a catalyst together with hydrogen, and is converted into methane by one or more chambers disposed inside the reactor. It is also possible to be synthesized.

In an embodiment of the present invention, the catalyst is used as an oxygen carrier particle of carbon monoxide or carbon dioxide based on a nickel component, so that it is possible to effectively react carbon monoxide or carbon dioxide with hydrogen.

In an embodiment of the present invention, carbon monoxide or carbon dioxide and hydrogen are flowed inside the reactor, and it is also possible to perform catalytic conversion reactions in each chamber from high temperature to low temperature by sequentially arranging chambers along the flow direction.

In an embodiment of the present invention, the chambers are composed of a first chamber, a second chamber, and a third chamber, wherein the first chamber is 400°C to 500°C, the second chamber is 350°C to 400°C, and the third chamber Is set to a temperature of 250 ℃ to 350 ℃ may be a carbon monoxide or carbon dioxide and hydrogen catalytic conversion reaction is performed.

In an embodiment of the present invention, the first chamber, the second chamber, and the third chamber are disposed inside one reactor, and biogas and hydrogen flow into one side of the reactor, and the first chamber inside the reactor , It may flow sequentially to the second chamber and the third chamber, and a catalytic conversion reaction is performed, so that methane and water may be discharged as a result of reacting to the other side of the reactor.

In an embodiment of the present invention, the energy independence system using pure oxygen combustion power and new and renewable energy uses the pure oxygen combustion power generation and renewable energy energy independence system as a base power in the island region. , It can be an island generator with an energy self-reliance system that improves energy independence by adding new and renewable energy.

According to an embodiment of the present invention, the energy independence system using pure oxygen combustion power and renewable energy is based on pure oxygen combustion power generation and adding new renewable energy, thereby renewing carbon monoxide or carbon dioxide generated in pure oxygen combustion power. By producing methane by combining with hydrogen generated by hydrolysis through renewable energy, energy can be supplied and supplied to improve energy independence.

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 block diagram of an energy independence system using pure oxygen combustion power generation and renewable energy according to an embodiment of the present invention.
2 is a block diagram of an energy self-reliance system using pure oxygen combustion power generation and renewable energy according to another embodiment of the present invention.
3 is a cross-sectional view showing a reactor to which an energy independence system using pure oxygen combustion power generation and renewable energy 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 block diagram of an energy self-reliance system using pure oxygen combustion power generation and renewable energy according to an embodiment of the present invention.

Referring to FIG. 1, the energy independence system 100 using pure oxygen combustion power generation and renewable energy according to the present invention includes a fuel supply unit 110 for supplying low-grade fuel, and a low supply supplied through the fuel supply unit 110. The low-grade fuel generation unit 120 that thermally decomposes grade fuel into an energy source to generate electricity, the renewable energy unit 130 that generates electricity through renewable energy, and the electricity produced through the renewable energy unit 130. Provided to reduce the pollutant emission source by supplying pure oxygen from the faucet dissection 140 or the outside during the generation of the faucet dissection 140 and the low-grade fuel generator 120 that are separated into hydrogen and oxygen by using in the faucet. Net oxygen supply unit 150, methanization unit 160 to methanize carbon monoxide or carbon dioxide produced through the low-grade fuel power generation unit 120 to produce methane by combining with hydrogen separated through the water receiving unit 140 ) And the methane processing unit 170 for collecting and storing the methane produced through the methanation unit 160 or transporting it to the outside.

In an embodiment of the present invention, it includes a fuel supply unit 110 for supplying low-grade fuel.

More specifically, the fuel supply unit 110 supplies at least one fuel among coal, biomass, and waste. Therefore, it is possible to reduce costs by supplying low-grade fuel to generate electricity.

In addition, a low-grade fuel generator 120 for thermally decomposing low-grade fuel supplied through the fuel supply unit 110 into an energy source is provided.

In more detail, the low-grade fuel generator 120 may be supplied with low-grade fuel through the fuel supply unit 110, and thermally decompose the low-grade fuel into an energy source to generate electricity, thereby producing electricity.

In addition, a new renewable energy unit 130 for producing electricity through renewable energy is provided.

More specifically, the new and renewable energy unit 130 is to generate electricity by using at least one of renewable energy such as wind power, water power, and solar power, without additional equipment or energy input, wind power, water power, and solar power. Can produce electricity.

In addition, a water electrolysis unit 140 for separating hydrogen and oxygen into electricity using the electricity produced through the renewable energy unit 130 is provided.

More specifically, the water electrolysis unit 140 electrolyzes water using electricity produced through the renewable energy unit 130, thereby separating oxygen and hydrogen. The renewable energy is preferably decomposed through surplus electricity to store oxygen and hydrogen and uses oxygen and hydrogen as necessary.

In addition, a pure oxygen supply unit 150 may be provided to reduce the pollutant emission source by supplying pure oxygen from the water receiving unit 140 or the outside when the low-grade fuel power generation unit 120 is generated.

In more detail, the pure oxygen supply unit 150 supplies oxygen produced by electrolyzing water through the faucet discharging unit 140 when generating the low-grade fuel power generation unit 120, or separately supplying oxygen from the outside. It is supplied and used for thermal decomposition of low-grade fuel.

Therefore, since pure oxygen is supplied through the pure oxygen supply unit 150, only water and carbon dioxide are generated during thermal decomposition of the low-grade fuel.

In addition, a methanation unit 160 is provided that combines carbon monoxide or carbon dioxide produced through the low-grade fuel power generation unit 120 with hydrogen separated through the water receiving unit 140 to methanize to produce methane.

In more detail, the methanation unit 160 may produce methane by combining carbon monoxide or carbon dioxide produced through the low-grade fuel power generation unit 120 with hydrogen and methanation.

That is, the low-grade fuel power generation unit 120 thermally decomposes the low-grade fuel as an energy source to produce carbon monoxide or carbon dioxide, and the water-removing unit 140 electrolyzes water to separate hydrogen. Therefore, methane can be produced by catalytically converting the carbon monoxide and carbon dioxide through hydrogen and a catalyst.

In addition, a methane processing unit 170 for collecting and storing methane produced through the methanation unit 160 or transporting it to the outside is provided.

More specifically, the methane processing unit 170 sends the methane produced through the methanation unit 160 to a storage or stores, or processes the methane to be used directly for household or industrial purposes.

In addition, the low-grade fuel includes at least one of coal, biomass, and waste, and continuously produces carbon monoxide or carbon dioxide through the low-grade fuel generation unit 120 to supply the methane to the methane stably. Can produce.

More specifically, the low-grade fuel generation unit 120 may continuously generate electricity through low-grade fuels such as coal, biomass, and waste, and produce carbon monoxide or carbon dioxide as a by-product. Accordingly, in the island region, the low-grade fuel power generation unit 120 is used as the base power generation, and carbon monoxide or carbon dioxide is reacted with hydrogen to produce methane, thereby generating additional energy and improving energy independence in the island region.

In addition, the faucet dissection 140 may generate electricity by using at least one of renewable energy such as wind power, water power, and sunlight.

In more detail, the faucet dissection 140 may utilize energy such as wind power, hydro power, and sunlight to produce electricity through renewable energy. Therefore, by utilizing renewable energy, it is possible to produce oxygen and hydrogen through water electrolysis without supply of additional energy.

In addition, the methanation unit 160 generates steam by using a large amount of heat generated in the process of producing methane by combining carbon monoxide or carbon dioxide with hydrogen, and generates steam by generating electricity through the steam. ) May be provided.

More specifically, a large amount of heat is generated in the reaction process during the catalytic conversion reaction of carbon monoxide or carbon dioxide and hydrogen in the methanation unit 160, and cooling is required for continuous reaction.

Accordingly, in the heat exchange process with the refrigerant, water may be heated by heating water through a refrigerant having a high temperature, or by using the refrigerant as water, hot water may be converted into steam to produce steam, and the steam generator 180 may The turbine can be rotated with steam to generate electricity.

In addition, the renewable energy unit 130 may generate electricity through renewable energy, and selectively store it in the battery 131.

More specifically, the new and renewable energy unit 130 can produce electricity through the new and renewable energy, and when the storage capacity of hydrogen or oxygen produced through electrolysis is full or no longer is required, production The electricity generated through the renewable energy can be stored in the battery 131, and can be used again for electrolysis if necessary.

In addition, the water faucet 140 does not supply oxygen and hydrogen separated through the water electrolysis to methane according to circumstances, but generates electricity through fuel cell power generation that generates electricity through the energy of oxidation and reduction reactions. The fuel cell power generation unit 190 may be provided.

More specifically, the water electrolysis unit 140 can separate oxygen and hydrogen through the water electrolysis, and reacts hydrogen and oxygen by reacting it in the fuel cell power generation unit 190 as necessary to produce electricity and heat. Can be. Therefore, the fuel cell power generation can improve energy efficiency and reduce the generation of greenhouse gas compared to the turbine power generation method using fossil fuel.

2 is a block diagram of an energy self-reliance system using pure oxygen combustion power generation and renewable energy according to another embodiment of the present invention.

Referring to FIG. 2, water used for the water dissipation unit 240 is supplied as seawater, and hydrogen separated through the water electrolysis is combined with carbon monoxide or carbon dioxide produced through the low-grade fuel power generation unit 220 to collect fresh water. Can produce.

In more detail, seawater may be supplied to the faucet dissection 240, and fresh water may be produced by combining the separated hydrogen with carbon monoxide or carbon dioxide produced through the low-grade fuel generation unit 220. Therefore, by supplying seawater to the faucet dissection 240 in an island region where water is insufficient, fresh water required for drinking water can be produced.

In addition, the catalyst may be used as an oxygen carrier particle of carbon monoxide or carbon dioxide based on a nickel component to effectively react carbon monoxide or carbon dioxide and hydrogen.

In addition, the methanation unit 260 is provided with a reactor such that carbon monoxide or carbon dioxide is synthesized into methane by a catalytic conversion reaction by a catalyst together with hydrogen, and may be synthesized into methane by one or more chambers disposed inside the reactor. .

In addition, carbon monoxide or carbon dioxide and hydrogen flow in the interior of the reactor, and the chambers are sequentially arranged along the flow direction, so that a catalytic conversion reaction can be performed in each chamber from high temperature to low temperature.

In addition, the chambers are composed of a first chamber, a second chamber, and a third chamber, the first chamber is 400°C to 500°C, the second chamber is 350°C to 400°C, and the third chamber is 250°C to 350°C. It is set to a temperature of carbon monoxide or carbon dioxide and hydrogen can be carried out catalytic conversion reaction.

In addition, the first chamber, the second chamber, and the third chamber are disposed inside one reactor, and biogas and hydrogen flow into one side of the reactor, such that the first chamber, the second chamber, and the third inside the reactor It is sequentially flowed into the chamber and a catalytic conversion reaction is performed, so that methane and water can be discharged as a result of reacting to the other side of the reactor.

3 is a cross-sectional view showing a reactor to which an energy independence system using pure oxygen combustion power generation and renewable energy according to an embodiment of the present invention is applied.

In one embodiment, the reactor may be provided as an integral multi-stage reactor for methanation. Referring to FIG. 3 in this regard, the integral multi-stage reactor 300 for methanation reacts carbon monoxide or carbon dioxide with hydrogen. In the reactor for the methanization by, the body portion 310 formed in the shape of a hollow tube so that gas flows therein, is disposed at the bottom of the interior of the body portion 310, carbon monoxide or a mixed gas composed of carbon dioxide and hydrogen And a first chamber 321 provided to cause a high temperature catalytic conversion reaction, provided at a lower end of the main body 310, and a supply unit 331 provided to supply a mixed gas to the lower end of the first chamber 321 , It is disposed between the supply unit 331 and the lower end of the first chamber 321, the carbon monoxide or carbon dioxide and hydrogen supplied from the supply unit 331 is provided to uniformly distribute the first chamber 321 1 gas distributor 341, the first heat exchange hopper is connected to the upper portion of the first chamber 321, and is provided to lower the temperature of the mixed gas flowing from the first chamber 321 by performing heat exchange through a refrigerant. (351), the second chamber is disposed on the top of the second gas separation unit, the second chamber is provided so that the catalytic conversion reaction with a catalyst consisting of carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber (321) ( 322), disposed between the bottom of the first heat exchange hopper 351 and the second chamber 322, the second, the carbon, water, carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber 321 The second gas distributor 342, which is provided to uniformly distribute to the chamber 322, is connected to the upper portion of the second chamber 322, and the temperature of the mixed gas flowed from the second chamber 322 through the refrigerant A second heat exchange hopper 361 provided to lower heat by performing heat exchange, a mixture of carbon monoxide or carbon dioxide and hydrogen disposed at the upper end of the third gas separation unit and flowing from the second chamber 322 A third chamber 323, which is provided to cause a catalytic conversion reaction with a suga catalyst, is disposed between the second heat exchange hopper 361 and the lower end of the third chamber 323, and the second chamber 322 The third gas distributor 343 is provided to uniformly distribute the carbon, water, carbon monoxide or carbon dioxide and hydrogen flowed therefrom to the third chamber 323, and is connected to the upper portion of the third chamber 323. 3 The third heat exchange hopper 371 is provided to lower the temperature of the mixed gas flowed from the chamber 323 by performing heat exchange through the refrigerant, and is provided at the top of the main body 310 to provide the third heat exchange hopper 371 It is disposed on the upper portion of the carbon monoxide or carbon dioxide and methane and water generated by the reaction of hydrogen and the catalyst to provide a discharge unit 332.

In an embodiment of the present invention, it includes a body portion 310 formed in a hollow tubular shape so that the gas flows therein.

More specifically, the body portion 310 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 310 and react to generate methane.

In addition, the first chamber 321 is disposed at the bottom of the inside of the main body 310 to cause a high temperature catalytic conversion reaction with a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen.

More specifically, the first chamber 321 is disposed at the bottom of the inside of the main body 310, 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 portion 310, a supply unit 331 is provided to supply a mixed gas to the bottom of the first chamber (321).

More specifically, the supply unit 331 is provided at the bottom of the main body 310 to supply a mixed gas composed of carbon oxide and hydrogen supplied from the outside to the first chamber 321. Therefore, the supply part 331 may be connected to the main body part 310 by means such as a tube and supplied to the first chamber 321.

In addition, it is disposed between the lower end of the supply unit 331 and the first chamber 321, the first gas to uniformly distribute the carbon monoxide or carbon dioxide and hydrogen supplied from the supply unit 331 to the first chamber 321 Dispenser 341 is provided.

More specifically, the first gas distributor 341 is disposed between the supply unit 331 and the lower end of the first chamber 321 inside the main body 310 to be supplied from the supply unit 331 It is provided to uniformly distribute the mixed gas to the first chamber (321). Therefore, the first gas distributor 341 uniformly distributes the mixed gas to effectively effect a catalytic conversion reaction.

In addition, the first heat exchange hopper 351 is provided to be connected to the upper portion of the first chamber 321 and to lower the temperature of the mixed gas flowing from the first chamber 321 by performing heat exchange through a refrigerant.

More specifically, the first heat exchange hopper 351 is connected to the upper portion of the first chamber 321 inside the main body 310 to cool the mixed gas and flows from the first chamber 321 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 322 is disposed on the upper end of the first heat exchange hopper 351, the mixed gas composed of carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber 321 to the catalytic conversion reaction with the catalyst ) Is provided.

More specifically, the second chamber 322 is disposed on the top of the first heat exchange hopper 351 inside the body portion 310, the carbon monoxide cooled through the first heat exchange hopper 351 or Methane is produced through a catalytic conversion reaction with a catalyst composed of carbon dioxide and hydrogen.

That is, in the second chamber 322, a mixed gas composed of carbon monoxide or carbon dioxide and hydrogen flowed from the first chamber 321 is cooled through the first heat exchange hopper 351, and the catalyst is converted through the catalyst. The reaction takes place.

In addition, carbon, water, carbon monoxide or carbon dioxide and hydrogen, which are disposed between the first heat exchange hopper 351 and the lower end of the second chamber 322, and flowed from the first chamber 321 are disposed in the second chamber ( A second gas distributor 342 is provided to uniformly distribute to the 322).

More specifically, the second gas distributor 342 is disposed between the lower end of the first heat exchange hopper 351 and the second chamber 322 inside the main body 310. It is provided to uniformly distribute the mixed gas flowed from the (351) to the second chamber (322). Therefore, the second gas distributor 342 uniformly distributes the mixed gas to effectively effect a catalytic conversion reaction.

In addition, a second heat exchange hopper 361 is provided to be connected to the upper portion of the second chamber 322 and to lower the temperature of the mixed gas flowing from the second chamber 322 by performing heat exchange through a refrigerant.

More specifically, the second heat exchange hopper 361 is connected to the upper portion of the second chamber 322 inside the main body 310 to cool the temperature of the mixed gas, the second chamber 322 The temperature of the mixed gas flowing therefrom is cooled by heat exchange through a refrigerant.

In addition, a third chamber 323 is provided to be disposed on the upper portion of the third gas separation unit, and a catalytic conversion reaction of the mixed gas composed of carbon monoxide or carbon dioxide and hydrogen flowed from the second chamber 322 occurs with the catalyst. .

The third chamber 323 is disposed on the top of the second heat exchange hopper 361 inside the main body 310, and is composed of carbon monoxide or carbon dioxide and hydrogen cooled through the second heat exchange hopper 361 Methane is produced through a catalytic conversion reaction with a mixed gas catalyst.

In addition, between the second heat exchange hopper 361 and the lower end of the third chamber 323, carbon, water, carbon monoxide or carbon dioxide and hydrogen flowed from the second chamber 322 are supplied to the third chamber ( A third gas distributor 343 is provided to uniformly distribute to 323).

More specifically, the third gas distributor 343 is disposed between the second heat exchange hopper 361 and the lower end of the third chamber 323 inside the main body 310. It is provided to uniformly distribute the mixed gas flowed from (361) to the third chamber (323). Therefore, the third gas distributor 343 uniformly distributes the mixed gas to effectively effect a catalytic conversion reaction.

In addition, a third heat exchange hopper 371 is provided to be connected to the upper portion of the third chamber 323 and to lower the temperature of the mixed gas flowing from the third chamber 323 by performing heat exchange through a refrigerant.

More specifically, the third heat exchange hopper 371 is connected to the upper portion of the third chamber 323 inside the main body 310 to cool the temperature of the mixed gas, the third chamber 323 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 310 is disposed on the upper portion of the third heat exchange hopper 371, carbon monoxide or carbon dioxide and methane and water generated by the reaction of the catalyst and the discharge portion 332 is discharged It is provided.

More specifically, the mixed gas composed of carbon monoxide or carbon dioxide and hydrogen introduced through the supply unit 331 provided at the bottom of the main body 310 is provided in the first chamber 321, the second chamber 322, and the third. It passes through the chamber 323 and reacts with the catalyst to generate methane and water, and is discharged through the discharge portion 332 formed on the top of the body portion 310.

At this time, the discharge unit 332 is connected by means such as a pipe and the top of the main body 310 to discharge methane and water.

In addition, the third heat exchange hopper 371 is disposed in a coiled long tube to lower the temperature of the mixed gas flowed from the third chamber 323, and the first refrigerant is introduced into one end so that the refrigerant flows therein An inlet 352 may be provided, and a first outlet 353 may be provided so that heat exchange is performed at the other end and refrigerant is discharged.

More specifically, the third heat exchange hopper 371 is formed of a coiled elongated tube, and a refrigerant flows therein, and the third heat exchange hopper 371 is transferred from the third chamber 323 by the refrigerant. The mixed gas flowing to the discharge unit 332 is cooled by heat exchange.

Therefore, at one end of the third heat exchange hopper 371, a first inlet 352 through which a refrigerant flows from the outside is provided, and the refrigerant introduced through the first inlet 352 passes through a tube formed in a coil shape. , Cooling the mixed gas passing through the outside of the third heat exchange hopper 371, and after the heat exchange is performed, is discharged through the first outlet 353 of the other end.

In addition, the second heat exchange hopper 361 is arranged in a coil-shaped long tube to lower the temperature of the mixed gas flowed from the second chamber 322, and the first outlet 353 at one end so that the refrigerant flows therein. ), a second inlet 362 through which the refrigerant flows is provided, and a second outlet 363 may be provided so that heat exchange is performed at the other end and the refrigerant is discharged.

More specifically, the second heat exchange hopper 361 is formed of a coiled elongated tube, and a refrigerant flows therein, and the second heat exchange hopper 361 is transferred from the second chamber 322 by the refrigerant. The mixed gas flowing into the third chamber 323 is cooled by heat exchange.

Therefore, a second inlet 362 through which a refrigerant flows from the first outlet 353 is provided at one end of the second heat exchange hopper 361 and connected to the first outlet 353, and the second inlet 362 ) By passing the refrigerant flowed through the tube formed in a coil shape, cools the mixed gas passing outside of the second heat exchange hopper 361, and after the heat exchange is performed, the second outlet 363 provided at the other end The refrigerant is discharged through.

In addition, the first heat exchange hopper 351 is arranged in a coil-shaped long tube to lower the temperature of the mixed gas flowed from the first chamber 321, the second outlet 363 at one end so that the refrigerant flows therein ), a third inlet 372 through which a refrigerant flows is provided, and a third outlet 373 may be provided so that heat exchange is performed at the other end and the refrigerant is discharged.

In more detail, the first heat exchange hopper 351 is formed of a coiled elongated tube, and a refrigerant flows therein, and the first heat exchange hopper 351 is transferred from the first chamber 321 by the refrigerant. The mixed gas flowing into the second chamber 322 is cooled by heat exchange.

Therefore, a third inlet 372 is provided at one end of the first heat exchange hopper 351 to be connected to the second outlet 363 and flow refrigerant through the second outlet 363, and the third inlet 372 ) 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 exchange hopper 351, and after the heat exchange is performed, a third outlet 373 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 321, and the mixed gas may be primarily cooled in the first heat exchange hopper 351.

In more detail, the first chamber 321 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 the catalyst introduced through the supply unit 331, and the heated mixed gas It is primarily cooled by the first heat exchange hopper 351. Therefore, the first chamber 321 is capable of efficiently producing methane by performing a catalytic conversion reaction at a high temperature.

In addition, in the second chamber 322, the mixed gas and catalyst cooled by the first heat exchange hopper 351 undergo a conversion reaction at a temperature of 350°C to 400°C, and are mixed in the second heat exchange hopper 361. The gas and catalyst can be cooled secondarily.

More specifically, in the second chamber 322, a mixed gas and a catalyst introduced through the first chamber 321 undergo a conversion reaction at a temperature of 350°C to 400°C, and the first chamber 321 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 secondarily cooled by the second heat exchange hopper 361 to efficiently produce methane.

In addition, in the third chamber 323, the mixed gas cooled by the second heat exchange hopper 361 and the catalyst undergo a conversion reaction at a temperature of 250°C to 350°C, and the mixed gas in the third heat exchange hopper 371 Can be cooled thirdly.

More specifically, in the third chamber 323, a mixed gas and a catalyst introduced through the second chamber 322 undergo a conversion reaction at a temperature of 250°C to 350°C, and the second chamber 322 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 exchange hopper 371 to efficiently produce methane.

In addition, the mixed gas passing through the first chamber 321, the second chamber 322, and the third chamber 323 is transferred to the first heat exchange hopper, the second heat exchange hopper 361 and the third heat exchange hopper 371. Therefore, it may be cooled sequentially and the temperature may gradually decrease.

More specifically, the first chamber 321, the second chamber 322 and the third chamber 323 are sequentially disposed inside the main body 310, the first chamber 321 and the first A first heat exchange hopper is disposed between the two chambers 322, a second heat exchange hopper is disposed between the third chambers 323 of the second chamber 322, and a first heat exchange hopper is disposed between the third chambers 323. A third heat exchange hopper is disposed, and the mixed gas passes sequentially through the first chamber 321, the second chamber 322, and the third chamber 323, and a catalytic conversion reaction is performed together with the catalyst, so that the first heat exchange The mixed gas is sequentially cooled through a hopper, a second heat exchange hopper 361 and a third heat exchange hopper 371.

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 exchange hopper 361 and the first heat exchange hopper 351, starting from the third heat exchange hopper, the third chamber 323, the second chamber 322 and the first chamber ( 321) may be sequentially heated to gradually increase the temperature.

In more detail, the third heat exchange hopper 371, the second heat exchange hopper 361 and the third heat exchange hopper 371 are connected to each other so that the refrigerant flows sequentially, and the refrigerant is the third chamber 323, the third As the two chambers 322 and the first chambers 321 are cooled, the temperature of the refrigerant gradually increases.

That is, the mixed gas is supplied to the bottom based on 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 310.

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 exchange hopper 351 may cool the first chamber 321 to heat the refrigerant having a temperature increase by heating the water generated through the reaction of carbon monoxide or carbon dioxide with hydrogen to produce steam.

More specifically, in the first chamber 321, a conversion reaction of a mixed gas and a catalyst occurs at a temperature of 400°C to 500°C, and the first heat exchange hopper 351 cools it.

Therefore, since the refrigerant of the first heat exchange hopper 351 maintains a high temperature, steam can be obtained by heating water through this, and steam produced through this can be sold or generated to generate electricity.

In addition, the integrated multi-stage reactor 300 for methanation may be applied to a 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 300 for methanation 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 catalyst high heat (reaction heat) at the same time as the reaction. 341), which is a formula for calculating the minimum fluidization rate according to the input of the catalyst through the second gas distributor 342 and the third gas distributor 343

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 input through the first gas distributor 341, the second gas distributor 342 and the third gas distributor 343, the flow rate and speed of carbon monoxide or carbon dioxide and hydrogen are controlled. Can be controlled.

The energy independence system using pure oxygen combustion power generation and new and renewable energy is equipped with an island generator with an energy independence system to improve energy independence by using pure oxygen combustion generators as base power in island areas and adding renewable energy. Can be.

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: Energy independence system using pure oxygen combustion power and renewable energy
110, 210: fuel supply unit
120, 220: low-grade fuel generation department
130, 230: Ministry of Renewable Energy
131, 231: battery
140, 240: faucet dissection
150, 250: pure oxygen supply
160, 260: methanation unit
170, 270: Methane treatment unit
180, 280: steam generator
190, 290: fuel cell power generation department
300: integral multi-stage reactor for methanation
310: main body
321 first chamber
322: second chamber
323: third chamber
331: supply
332: outlet
341: first gas distributor
342: second gas distributor
343: third gas distributor
351: first heat exchange hopper
352: first inlet
353: first outlet
361: second heat exchange hopper
362: second inlet
363: second outlet
371: third heat exchange hopper
372: third inlet
373: third outlet

Claims (13)

A fuel supply unit that supplies low-grade fuel;
A low-grade fuel generator that communicates with the fuel supply unit and generates electricity by thermally decomposing low-grade fuel supplied through the fuel supply unit into an energy source while supplying carbon monoxide or carbon dioxide to the methanation unit;
A new and renewable energy department that produces electricity through renewable energy;
A water electrolysis unit electrically connected to the renewable energy unit and separating hydrogen and oxygen into electricity using the electricity produced through the renewable energy unit;
It is provided to communicate with the faucet and the low-grade fuel generator and supply the oxygen introduced from the faucet or pure oxygen from the outside to the low-grade fuel generator when the low-grade fuel generator is generated to reduce pollution sources. Pure oxygen supply unit;
It communicates with the low-grade fuel generation unit and the faucet, and generates steam using a large amount of heat generated in the process of producing methane by combining the carbon monoxide or the carbon dioxide with hydrogen, and generates electricity through the steam to generate electricity. A methanation unit having a steam generating unit for producing and methanizing the carbon monoxide or the carbon dioxide produced through the low-grade fuel generating unit with hydrogen separated through the water receiving unit to produce methane; And
A methane treatment unit communicating with the methanation unit and collecting and storing methane produced through the methanation unit and transporting it to the outside;
Including,
The low-grade fuel generation unit supplies the carbon monoxide or the carbon dioxide to the methanation unit while producing the electricity,
The pure oxygen supply unit supplies the oxygen or the pure oxygen to a low-grade fuel power generation unit,
The water electrolysis unit supplies the hydrogen to the methanation unit,
The methanation unit supplies the steam to the steam generator while supplying the methane to the methane processing unit,
Accordingly, the methanation unit and the steam generation unit supply the electricity to the island area, and the methane processing unit sends the methane to a storage area or processes the methane to be used for home or industrial use and supplies it to the island area. An energy independence system that uses pure oxygen-fired power generation and renewable energy to improve local energy independence. The low-grade fuel comprises at least one of coal, biomass, and waste, and continuously produces carbon monoxide or carbon dioxide through the low-grade fuel power generation unit and supplies it to the methanation unit to stably supply methane. Energy independence system using pure oxygen combustion power generation and new and renewable energy, characterized by producing. The system of claim 1, wherein the renewable energy unit generates electricity using at least one of the renewable energy, wind power, hydro power, and solar power. delete The energy independence system using pure oxygen combustion power generation and renewable energy according to claim 1, wherein the renewable energy unit generates electricity through renewable energy and selectively stores it in a battery. The method of claim 1, wherein the water electrolysis unit does not supply oxygen and hydrogen separated through the water electrolysis to methane according to circumstances, but generates electricity through fuel cell power generation that generates electricity through the energy of oxidation and reduction reactions. An energy independence system using pure oxygen-fired power generation and renewable energy, characterized in that a fuel cell power generation unit is produced. The method of claim 1, characterized in that the water used for the electrolysis section is supplied to seawater, and hydrogen separated through the electrolysis section is combined with carbon monoxide or carbon dioxide produced through the low-grade fuel generation section to produce fresh water. Energy independence system using pure oxygen combustion power and renewable energy. The method of claim 1, wherein the methanation unit is provided with a reactor such that carbon monoxide or carbon dioxide is synthesized into methane by a catalytic conversion reaction by a catalyst with hydrogen, and is synthesized into methane by one or more chambers disposed inside the reactor. Energy independence system using pure oxygen combustion power generation and renewable energy. 10. The method according to claim 8, wherein the catalyst is used as an oxygen carrier particle of carbon monoxide or carbon dioxide based on a nickel component, so that carbon monoxide or carbon dioxide and hydrogen react effectively, pure oxygen combustion power and energy independence using renewable energy system. 10. The method of claim 9, Carbon monoxide or carbon dioxide and hydrogen flow in the interior of the reactor, the chamber is sequentially arranged along the flow direction, the catalytic conversion reaction is carried out in each chamber from high temperature to low temperature combustion Energy independence system using power generation and renewable energy. ◈ Claim 11 was abandoned when payment of the set registration fee was made.◈ 11. The method of claim 10, The chamber is composed of a first chamber, a second chamber and a third chamber, the first chamber is 400 ℃ ~ 500 ℃, the second chamber is 350 ℃ ~ 400 ℃ and the third chamber is 250 Energy independence system using pure oxygen combustion power generation and renewable energy, characterized in that the catalytic conversion reaction of carbon monoxide or carbon dioxide and hydrogen is performed at a temperature of ℃~350℃. ◈ Claim 12 was abandoned when payment of the set registration fee was made.◈ 12. The method of claim 11, The first chamber, the second chamber and the third chamber are disposed inside one reactor, biogas and hydrogen are introduced into one side of the reactor, the first chamber, the first chamber inside the reactor Energy independence system using pure oxygen combustion power generation and renewable energy, characterized in that methane and water are discharged as a result of reacting to the other side of the reactor through a catalytic conversion reaction performed sequentially in the second chamber and the third chamber. According to claim 1, the energy independence system using the pure oxygen combustion power generation and new renewable energy is characterized by using the pure oxygen combustion generator as a base power generation in the island region, and adding new and renewable energy to improve the energy independence An island generator with an energy self-reliance system.

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