KR102510675B1 - Fuel cell generation system and vessel including the same - Google Patents

Abstract

A fuel cell power generation system according to the present invention includes a hydrogen production unit (100) that produces hydrogen by decomposing gaseous ammonia, and a hydrogen fuel cell unit (200) that produces power using hydrogen produced by the hydrogen production unit (100). ), wherein the hydrogen production unit 100 converts an ammonia decomposer 110 that thermally decomposes the gaseous ammonia, and a mixed gas including undecomposed ammonia discharged from the ammonia decomposer 110, hydrogen, and nitrogen into the hydrogen A first heat exchanger 171 is provided to increase the temperature of the mixed gas by exchanging heat with the first exhaust gas EG1 generated from the fuel cell unit 200 .

Description

Fuel cell power generation system and vessel equipped with the same system {FUEL CELL GENERATION SYSTEM AND VESSEL INCLUDING THE SAME}

The present invention relates to a fuel cell power generation system and a ship equipped with the same system, and more particularly, to a fuel cell power generation system that reduces overall energy consumption and maximizes efficiency while using ammonia, and to a ship equipped with the system.

As carbon dioxide (CO ₂ ) emitted into the atmosphere is pointed out as the key to global warming, a broad hydrogen economic cycle using hydrogen as fuel to replace fossil fuels centered on hydrocarbons that emit carbon dioxide during combustion, that is, the production and transportation of hydrogen , and various methods of combustion are being explored.

Industrially, hydrogen is mainly produced using steam methane reformer (SMR) or methanol reforming, but due to the nature of raw materials containing carbon, carbon dioxide is inevitably released during the process. When hydrogen is produced by electrolysis of water, carbon dioxide is not generated, but the production cost is high compared to the above method, so it is used on a small scale. Hydrogen has the smallest molecular weight among elements and has a low weight per unit volume and a very low boiling point of -259.2 ° C, so there are many technical and commercial difficulties in liquefaction, storage and transportation. That is, hydrogen liquefaction is essential for large-scale transportation by sea, and the difficulty of condensing liquid hydrogen boil-off gas (BOG) is high. It is not easy to activate the hydrogen economy due to the increase in transportation cost per unit weight.

Therefore, a fuel cell power generation system that produces hydrogen by decomposing ammonia, which is easy to operate, and generates electric power using the produced hydrogen, has been developed.

In such a fuel cell power generation system, high-temperature exhaust gas is generated, and since it is discharged to the outside, there is a problem in that overall energy consumption increases.

A technical problem to be achieved by the spirit of the present invention is to provide a fuel cell power generation system that reduces overall energy consumption and maximizes efficiency while using ammonia and a ship equipped with the system.

A fuel cell power generation system according to an aspect of the present invention includes a hydrogen production unit 100 that produces hydrogen by decomposing gaseous ammonia, and a hydrogen fuel cell that generates power using the hydrogen produced by the hydrogen production unit 100. It includes a unit 200, wherein the hydrogen production unit 100 includes an ammonia decomposer 110 for thermally decomposing the gaseous ammonia, and a mixed gas including undecomposed ammonia discharged from the ammonia decomposer 110, hydrogen, and nitrogen. and a first heat exchanger 171 that heats up the mixed gas by exchanging heat with the first exhaust gas EG1 generated from the hydrogen fuel cell unit 200.

In addition, the first exhaust gas EG1 passing through the first heat exchanger 171 may be branched at the first branching point 10 and joined to the front end 20 of the first heat exchanger.

In addition, a heater may be further included at the front or rear end of the first heat exchanger 171 .

In addition, the hydrogen fuel cell unit 200 passes through the first heat exchanger 171 and pressurizes the fuel cell unit 210 that generates power using the hydrogen contained in the heated mixed gas as fuel. The compressor 220 supplied to the fuel cell unit 210, and the air pressurized by the compressor 220 are heat-exchanged with the second exhaust gas EG2 generated in the fuel cell unit 210 to heat the fuel cell It may include a second heat exchanger 230 supplying the high-temperature and high-pressure air to the branch 210 .

In addition, the hydrogen production unit 100 may further include a combustor 180 generating third exhaust gas EG3 by burning the first exhaust gas EG1 passing through the first heat exchanger 171. can

In addition, the third exhaust gas EG3 may be supplied to the ammonia decomposer 110 for heat exchange.

In addition, the hydrogen production unit 100 further includes an ammonia storage tank 160 for storing liquid ammonia, and a vaporizer 150 for vaporizing the liquid ammonia and supplying it to the ammonia decomposer 110, The third exhaust gas EG3 passing through 110 may be supplied to the vaporizer 150 to exchange heat.

In addition, the hydrogen production unit 100 may further include an ammonia adsorber 120 for adsorbing the undecomposed ammonia in the mixed gas discharged from the ammonia decomposer 110.

In addition, the ammonia adsorber 120 is a heating alternating adsorber, and each of the first tube 331 and the second tube 332, the first tube 331 and the second tube 332 are spaced apart from each other. A first tube tube 333 connected to the inside, and a second tube tube 334 connected to contact or connect to the outer surface of each of the first tube 331 and the second tube 332 to enable heat exchange can include

In addition, the first tube 331 and the second tube 332 are alternately introduced into the first tube 331 and the second tube 332 through the first tube 333. The undecomposed ammonia is adsorbed from the mixed gas, and the first tube 331 and the second tube 332 pass through the second tube tube 334 to the first tube 331 and the second tube ( 332) may be contacted or connected to the outer surface of the mixed gas to be alternately heat exchanged and regenerated.

In addition, the second tube tube 334 includes a front-end second tube tube 3341 connected to the ammonia decomposer 110 and a rear-end second tube tube 3342 connected to the third heat exchanger 130. can do.

In addition, the mixed gas supplied from the ammonia decomposer 110 to the ammonia adsorber 120 through the front end second tube 3341 exchanges heat with the first tube 331 or the second tube 332 The first tube 331 or the second tube 332 is regenerated and supplied to the third heat exchanger 130 through the second tube 3342 at the rear end.

In addition, the mixed gas supplied to the third heat exchanger 130 through the rear end second tube 3342 may be cooled in the third heat exchanger 130 .

In addition, the first tube tube 333 includes a front end tube tube 3331 connected to the third heat exchanger 130, and the mixed gas discharged from the first heat exchanger 130 is It is supplied to the inside of the first tube 331 or the second tube 332 through the first tube tube 3331 at the front end, and the undecomposed ammonia in the first tube 331 or the second tube 332 is can be adsorbed.

In addition, the first tube 333 further includes a rear end first tube 3332 connected to the first heat exchanger 171, and the hydrogen and nitrogen included in the mixed gas are It may be supplied to the first heat exchanger 171 through the first tube 3332 and exchange heat with the first exhaust gas EG1.

A vessel according to another aspect of the present invention may include the fuel cell power generation system described above.

At this time, the ship may be an ammonia carrier or an ammonia fuel propulsion ship.

The fuel cell power generation system according to an embodiment of the present invention is environmentally friendly because hydrogen is produced by decomposing ammonia that does not emit carbon dioxide and electricity is generated using the produced hydrogen.

In addition, by raising the temperature of the mixed gas discharged from the ammonia decomposer in which ammonia is reformed at a low temperature using the first heat exchanger in which heat is exchanged with the first exhaust gas generated in the fuel cell unit, the operation of the fuel cell unit operating at a high temperature is improved. By making it smoothly, it is possible to increase the power production efficiency of the fuel cell unit.

In addition, since the high-temperature third exhaust gas generated from the combustor can be used as a heat source for the ammonia decomposer and the vaporizer, it is economical by reducing overall energy consumption.

In addition, the second heat exchanger of the hydrogen fuel cell unit may supply high-temperature and high-pressure air to the fuel cell unit by exchanging heat with the high-temperature exhaust gas generated from the fuel cell unit for the high-pressure air pressurized by the compressor. Therefore, it is possible to increase the power production efficiency of the fuel cell unit by smoothly performing the reduction reaction of oxygen in the cathode unit of the fuel cell unit.

1 is a specific diagram of a fuel cell power generation system according to an embodiment of the present invention.
2 is a specific diagram of a fuel cell power generation system according to another embodiment of the present invention.
FIG. 3 is a detailed view of the ammonia adsorber of FIG. 2 .
FIG. 4 is a view explaining a state in which the first tube adsorbs undecomposed ammonia and the second tube is regenerated in the ammonia adsorber of FIG. 2 .
FIG. 5 is a view explaining a state in which the second tube adsorbs undecomposed ammonia and the first tube is regenerated in the ammonia adsorber of FIG. 2 .

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings so that those skilled in the art can easily carry out the present invention. This invention may be embodied in many different forms and is not limited to the embodiments set forth herein.

1 is a specific diagram of a fuel cell power generation system according to an embodiment of the present invention.

As shown in FIG. 1, the fuel cell power generation system according to an embodiment of the present invention includes a hydrogen production unit 100 that produces hydrogen by decomposing liquid ammonia (L-NH ₃ ), and a hydrogen production unit. The main point is to provide a fuel cell power generation system that reduces overall energy consumption and maximizes efficiency while using ammonia, including a hydrogen fuel cell unit 200 that generates power using hydrogen produced in (100).

The fuel cell power generation system according to an embodiment of the present invention may be installed on a ship, where the ship may be an ammonia carrier or an ammonia fuel propulsion ship.

The hydrogen production unit 100 includes a vaporizer 150, an ammonia decomposer 110, a first heat exchanger 171, a blower 172, a combustor 180, and an ammonia storage tank 160. can include

The vaporizer 150 may vaporize liquid ammonia (L-NH ₃ ) into gaseous ammonia (G-NH ₃ ). In this case, the high-temperature third exhaust gas EG3 discharged from the combustor 180 may be used as a heat source, as will be described later.

The vaporizer 150 may be a shell and tube type heat exchanger. However, it is not necessarily limited thereto, and heat exchangers of various structures are possible.

The ammonia decomposer 110 may reform the gaseous ammonia (G-NH ₃ ) generated in the vaporizer 150 by thermally decomposing it. That is, the ammonia cracker 110 may decompose gaseous ammonia (G-NH ₃ ) passing through the vaporizer 150 into hydrogen (H ₂ ) and nitrogen (N ₂ ) through a cracking reformer. At this time, undecomposed undecomposed ammonia (NH ₃ ) may be generated. In this case, the high-temperature third exhaust gas EG3 discharged from the combustor 180 may be used as a heat source, as will be described later.

In addition, the ammonia decomposer 110 may include an ammonia decomposition catalyst so that ammonia can be reformed at a lower temperature. The ammonia decomposition catalyst is not particularly limited as long as it has a catalytic activity for the ammonia decomposition reaction, but examples thereof include catalysts containing a non-metal-based transition metal, a rare earth-based material, and a noble metal-based material as a composition. It can be used while supported on a carrier having a specific surface area.

Specifically, the low-temperature catalytic ammonia reformer (decomposer) is an ammonia reformer capable of decomposing ammonia at a low temperature, for example, about 400 to 600 ° C. may be included as a decomposition catalyst. These decomposition catalysts are not limited to the above-mentioned elements, and may include copper oxide, chromium oxide, manganese oxide, iron oxide, palladium, or platinum. Alternatively, it may be a decomposition catalyst in which chromium, copper or cobalt is supported on zeolite.

The amount of heat used for ammonia reforming can be minimized by using the ammonia reformer 110 of a low-temperature catalyst type.

Meanwhile, in the ammonia decomposer 110, ammonia reforming is performed at a relatively low temperature, but since the fuel cell unit 210 of the hydrogen fuel cell unit 200 operates at a relatively high temperature, fine particles discharged from the ammonia decomposer 110 Therefore, it is necessary to raise the temperature of the mixed gas containing ammonia, hydrogen and nitrogen.

Therefore, the first heat exchanger 171 heats the mixed gas discharged from the ammonia decomposer 110 with the first exhaust gas EG1 generated from the hydrogen fuel cell unit 200 to increase the temperature of the mixed gas. Although not shown, by additionally providing a separate heater at the front or rear end of the first heat exchanger 171, the load on the first heat exchanger 171 required to raise the temperature of the mixed gas is reduced, and at the same time, a multi-stage heating furnace fuel cell The temperature may be raised to a temperature suitable for the branch 210 .

That is, the first exhaust gas EG1 containing some of unreacted hydrogen, nitrogen, and some of water vapor resulting from electrochemical reaction in the fuel cell unit 210 of the hydrogen fuel cell unit 200 is generated. . At this time, the first exhaust gas EG1 is heat-exchanged with the mixed gas in the first heat exchanger 171 to increase the temperature of the mixed gas, and the first exhaust gas EG1 passing through the first heat exchanger 171 is Along with supplying thermal energy to the combustor 180, it can be combusted.

The blowing unit 172 diverges some of the first exhaust gas EG1 passing through the first heat exchanger 171 at the first branching point 10 and joins it to the front end 20 of the first heat exchanger to re-energize the fuel cell. It can be recycled as a fuel for branch 210 to improve energy efficiency. Here, the blowing means 172 may be a blower.

A portion of the first exhaust gas EG1 passing through the first heat exchanger 171 is branched at the first branching point 10 and joined to the front end 20 of the first heat exchanger, whereby thermal energy of high-temperature combustion products is obtained. It can also be prevented from supplying unreacted hydrogen and nitrogen more than necessary to the combustor 180 that generates .

That is, it is possible to prevent the supply of unreacted hydrogen and nitrogen to the combustor 180 in excess of the required amount of fuel capable of satisfying the temperature conditions of the ammonia decomposer 110 and the vaporizer 150, thereby increasing energy efficiency. be able to

The first branch point 10 may be located on the flow of the first exhaust gas EG1 between the first heat exchanger 171 and the combustor 180 .

The combustor 180 may burn the first exhaust gas EG1 passing through the first heat exchanger 171 to generate a high-temperature combustion product, the third exhaust gas EG3.

The high-temperature third exhaust gas EG3 is supplied to the ammonia decomposer 110 and heat-exchanged, so that it can be used as a heat source for the ammonia decomposer 110 . In addition, the third exhaust gas EG3 passing through the ammonia decomposer 110 is sequentially supplied to the vaporizer 150 and heat-exchanged, so that it can be used as a heat source of the vaporizer 150.

In this way, the third exhaust gas EG3 passes through the ammonia decomposer 110 and the vaporizer 150, and is cooled to 100° C. or less and discharged to the outside as medium-temperature exhaust gas, thereby ensuring safety.

The combustor 180 is not particularly limited as long as it can burn hydrogen, and may be, for example, a combustion reaction device including a combustion catalyst therein, or a direct combustion device.

The ammonia storage tank 160 is a tank capable of storing liquid ammonia, and may be a membrane type tank or an independent tank, and in the case of an independent tank, it may be an IMO type A, IMO type B, or IMO type C storage tank. there is. However, it is not necessarily limited thereto, and storage tanks of various structures are possible.

In addition, although not shown, a supply pump for supplying liquid ammonia may be installed inside the ammonia storage tank 160 . The feed pump may be a submerged pump or a deep well pump installed in liquid ammonia.

Meanwhile, the hydrogen fuel cell unit 200 may include a fuel cell unit 210, a compressor 220, and a second heat exchanger 230.

The fuel cell unit 210 is a fuel cell that uses hydrogen as fuel and is not particularly limited in shape, but is preferably a solid oxide fuel cell (SOFC) or a high temperature polymer electrolyte fuel cell, which is a high temperature fuel cell. (Polymer Electrolyte Membrane Fuel Cell; PEMFC). A fuel cell refers to an energy conversion cell that directly converts chemical energy of fuel gas into electrical energy. The fuel cell unit 210 may generate electric power by utilizing hydrogen among the mixed gases heated up while passing through the first heat exchanger 171 .

The fuel cell unit 210 includes an anode unit 211 in which an oxidation reaction of hydrogen occurs, a cathode unit 212 in which a reduction reaction of oxygen occurs, and electrons generated by an oxidation reaction of hydrogen in the anode unit 211 are a cathode unit. A wire connecting the anode part 211 and the cathode part 212 to move to the part 212 may be included. Hydrogen produced in the hydrogen production unit 100 may be supplied as fuel to the anode part 211 , and air containing oxygen may be supplied to the cathode part 212 .

At this time, the space between the anode part 211 and the cathode part 212 is filled with the electrolyte 213, and hydrogen cations generated by the oxidation reaction of hydrogen in the anode part 211 pass through the electrolyte 213 to the cathode part ( 212) to move. At this time, an oxidation catalyst that promotes the oxidation of hydrogen may be additionally used.

The shape of the fuel cell unit 210 is not limited to the above example, and various materials used in the fuel cell unit 210, for example, materials constituting the anode and cathode, types of electrolytes and catalysts, etc. Not particularly limited. The power generated by the fuel cell unit 210 may be supplied to various sources, and may be used, for example, for power such as the compressor 220 to be described later. In addition, when the fuel cell power generation system according to an embodiment of the present invention is provided in a ship, it can be supplied to various power demand places of the ship.

Meanwhile, the high-temperature second exhaust gas EG2 is generated by the electrochemical reaction in the fuel cell unit 210, and the high-temperature second exhaust gas EG2 is generated by the second heat exchanger 230 and the combustor ( 180 to supply heat energy to the second heat exchanger 230 and the combustor 180 in turn.

The compressor 220 may pressurize air and supply it to the cathode part 212 of the fuel cell part 210 .

At this time, the second heat exchanger 230 may be located on the flow of air transported between the compressor 220 and the fuel cell unit 210 . The second heat exchanger 230 heat-exchanges the high-pressure air pressurized by the compressor 220 with the oxygen-depleted second exhaust gas EG2 generated in the fuel cell unit 210 to form a cathode of the fuel cell unit 210. High-temperature and high-pressure air may be supplied to the unit 212 . Therefore, since the oxygen reduction reaction is smoothly performed in the cathode unit 212 , power generation efficiency in the fuel cell unit 210 may be increased.

Meanwhile, in the above embodiment, undecomposed ammonia may be input into the fuel cell unit, but other embodiments in which an ammonia adsorber for separating undecomposed ammonia is installed are also possible.

Hereinafter, a fuel cell power generation system according to another embodiment of the present invention will be described in detail with reference to FIGS. 2 to 5 .

2 is a specific diagram of a fuel cell power generation system according to another embodiment of the present invention.

The other embodiment shown in FIG. 2 is substantially the same as the one shown in FIG. 1 except for the structure of the ammonia adsorber, so repeated description is omitted.

As shown in FIG. 2, the hydrogen production unit 100 of the fuel cell power generation system according to another embodiment of the present invention includes a vaporizer 150, an ammonia decomposer 110, an ammonia adsorber 120, a third heat exchanger ( 130), a first heat exchanger 171, a blower 172, a combustor 180, and an ammonia storage tank 160.

The ammonia adsorber 120 may adsorb undecomposed ammonia (NH ₃ ) from a mixed gas containing undecomposed ammonia, hydrogen, and nitrogen discharged from the ammonia decomposer 110 .

That is, the ammonia adsorber 120 may adsorb undecomposed ammonia (NH ₃ ) discharged from the ammonia decomposer 110 . The ammonia adsorber 120 may be a temperature swing adsorber or a thermal swing adsorption (TSA). The alternating heating adsorber may have a structure in which impurities are adsorbed and when saturation is reached, heat is applied to regenerate the adsorber.

The ammonia adsorption material of the ammonia adsorber 120 is not particularly limited as long as it can adsorb undecomposed ammonia and can be regenerated in a saturated state, but preferably includes adsorption containing any one of zeolite, activated carbon, alumina, and silica. It may be a material or a composite oxide thereof.

Meanwhile, in order to adsorb undecomposed ammonia (NH ₃ ) in the ammonia adsorber 120, the undecomposed ammonia needs to be cooled. The third heat exchanger 130 cools the mixed gas including undecomposed ammonia, hydrogen, and nitrogen to make it easy to adsorb undecomposed ammonia (NH ₃ ) in the ammonia adsorber 120 .

The third heat exchanger 130 can cool the undecomposed ammonia to about 40 ° C. or less, preferably to the ambient temperature level, in order to adsorb the high-temperature undecomposed ammonia from the ammonia decomposer 110 in the ammonia adsorber 120. . The cooling method of the third heat exchanger 130 is not particularly limited, but may be, for example, an air cooling method, a water cooling method, or a method using a separate refrigerant.

3 is a detailed view of an ammonia adsorber of a fuel cell power generation system according to an embodiment of the present invention, and FIG. 4 is a state in which a first tube adsorbs undecomposed ammonia and a second tube is regenerated in the ammonia adsorber of FIG. 3 , and FIG. 5 is a view explaining a state in which the second tube adsorbs undecomposed ammonia and the first tube is regenerated in the ammonia adsorber of FIG. 2 .

As shown in FIG. 3, the ammonia adsorber 120 is spaced apart from each other into the first tube 331 and the second tube 332, the first tube 331 and the second tube 332, respectively. The first tube tube 333, the first tube 331 and the second tube 332 are connected to each other in contact with or connected to the outer surface of the second tube tube 334 to proceed with the heat exchange process, the first tube tube ( It may include a first valve 335 installed in 333, and a second valve 336 installed in second tube pipe 334.

The first tube tube 333 includes a first tube tube 3331 at the front end connected to the third heat exchanger 130 and a first tube tube 3332 at the rear end connected to the first heat exchanger 171 at the rear end. can do. And, the second tube tube 334 may include a second tube tube 3341 at the front end connected to the ammonia decomposer 110 and a second tube tube 3342 at the rear end connected to the third heat exchanger 130. there is.

The first tube 331 and the second tube 332 may adsorb undecomposed ammonia alternately introduced into the first tube 331 and the second tube 332 through the first tube 333. . In addition, the first tube 331 and the second tube 332 contact or are connected to the outer surfaces of the first tube 331 and the second tube 332 through the second tube tube 334 to alternately exchange heat, It can be regenerated by a high-temperature mixed gas containing undecomposed ammonia, hydrogen and nitrogen.

This will be described in detail with reference to FIGS. 4 and 5 below.

First, as shown in FIG. 4, the first tube 331 is mixed with undecomposed ammonia, hydrogen, and nitrogen introduced through the first front end tube 3331 connected to the third heat exchanger 130. When adsorbing undecomposed ammonia in the gas, the second tube 332 exchanges heat with a mixed gas including high-temperature undecomposed ammonia, hydrogen, and nitrogen flowing from the ammonia decomposer 110 through the second front end tube 3341. and can be reproduced. Through this, the mixed gas containing high-temperature undecomposed ammonia, hydrogen, and nitrogen is firstly cooled. The second tube 332 adsorbs undecomposed ammonia in the previous process and regenerates it by exchanging heat with a mixed gas containing high-temperature undecomposed ammonia, hydrogen, and nitrogen flowing through the second tube 3341 in a saturated state. It can be.

Meanwhile, since undecomposed ammonia (NH ₃ ) is adsorbed to the first tube 331, only hydrogen and nitrogen are discharged from the first tube 331, and hydrogen and nitrogen discharged from the first tube 331 are discharged from the second tube 331. It may be introduced into the first heat exchanger 171 through one tube 3332. In addition, the mixed gas including high-temperature undecomposed ammonia, hydrogen, and nitrogen from which the second tube 332 is regenerated may be put into the third heat exchanger 130 through the second tube 3342 at the rear end and cooled. . At this time, the mixed gas containing high-temperature undecomposed ammonia, hydrogen, and nitrogen may be secondarily cooled to a temperature of about 40 degrees or less, preferably atmospheric temperature. Therefore, the ammonia adsorber 120 is in a state where it is easy to adsorb undecomposed ammonia (NH ₃ ).

Next, as shown in FIG. 5, the mixed gas containing undecomposed ammonia, hydrogen, and nitrogen that has passed through the third heat exchanger 130 is transferred to the second tube 332 regenerated in FIG. The undecomposed ammonia introduced through the tube 3331 may be adsorbed in the second tube 332 . Since undecomposed ammonia is adsorbed in the second tube 332, only hydrogen and nitrogen are discharged from the second tube 332, and the hydrogen and nitrogen discharged from the second tube 332 are discharged through the first tube 3332 at the rear end. It may be introduced into the first heat exchanger 171 through. At this time, the first tube 331 receives heat from a mixed gas containing high-temperature undecomposed ammonia, hydrogen, and nitrogen flowing from the ammonia decomposer 110 through the second front end tube 3341 (heat exchanged). can be played At this time, as described above, the mixed gas containing high-temperature undecomposed ammonia, hydrogen, and nitrogen is firstly cooled. In addition, the mixed gas including high-temperature undecomposed ammonia, hydrogen, and nitrogen from which the first tube 331 is regenerated may be put into the third heat exchanger 130 through the second tube 3342 at the rear end and cooled. there is. At this time, the mixed gas containing high-temperature undecomposed ammonia, hydrogen, and nitrogen may be secondarily cooled to a temperature of about 40 degrees or less, preferably atmospheric temperature. Therefore, the ammonia adsorber 120 is in a state where it is easy to adsorb undecomposed ammonia (NH ₃ ).

Although not shown, when undecomposed ammonia (NH ₃ ) adsorbed to the first tube 331 or the second tube 332 is desorbed in the regeneration process, the undecomposed ammonia passes through a blowing means such as a blower to the ammonia decomposer 110 It can be put into the front end of and recycled. Through this, by recycling the undecomposed ammonia desorbed in the ammonia regeneration process by inputting it to the front end of the ammonia reformer 110, it is possible to reduce operating costs.

The first valve 335 is installed in the first tube pipe 333 to adjust the amount of the mixed gas containing undecomposed ammonia flowing through the first tube pipe 333 . Similarly, the second valve 336 is installed in the second tube 334 to adjust the amount of the mixed gas containing undecomposed ammonia flowing through the second tube 334 .

As such, when the regeneration process is performed in the first tube 331, the adsorption process is performed in the second tube 332, and when the adsorption process is performed again in the first tube 331, the second tube 332 ) By proceeding with the regeneration process, the ammonia adsorber 120 can be efficiently used.

In this embodiment, the ammonia adsorber 120 is composed of only the first tube 331 and the second tube 332, but is not necessarily limited thereto, and the ammonia adsorber 120 is composed of three, four or more tubes. It is also possible.

Meanwhile, the first heat exchanger 171 transfers the mixed gas containing hydrogen and nitrogen discharged from the ammonia adsorber 120 to the high-temperature first exhaust gas EG1 generated from the fuel cell unit 210 and the first heat exchanger. The temperature can be raised by heat exchange through (171). Although not shown, by additionally providing a separate heater at the front or rear end of the first heat exchanger 171, the load on the first heat exchanger 171 required to raise the temperature of the mixed gas is reduced, and at the same time, a multi-stage heating furnace fuel cell The temperature may be raised to a temperature suitable for the branch 210 .

In addition, some of the first exhaust gas EG1 passing through the first heat exchanger 171 is branched at the first branching point 10 and joined to the front end 20 of the first heat exchanger to return to the fuel cell unit 210. can be recycled as fuel.

As described above, since the fuel cell power generation system according to another embodiment of the present invention can adsorb undecomposed ammonia using an ammonia adsorber, it is possible not to supply undecomposed ammonia to the fuel cell unit, thereby preventing corrosion of the fuel cell unit. can do.

In the above, the present invention has been described with reference to the embodiments shown in the drawings. However, the present invention is not limited thereto, and various modifications or other embodiments belonging to the scope equivalent to the present invention can be made by those skilled in the art. Therefore, the true scope of protection of the present invention will be defined by the following claims.

100: hydrogen production unit 110: ammonia cracker
120: ammonia adsorber 130: third heat exchanger
150: vaporizer 160: ammonia storage tank
171: first heat exchanger 172: blowing means
180: combustor 200: hydrogen fuel cell unit
210: fuel cell unit 220: compressor
230: second heat exchanger

Claims (17)

A hydrogen production unit 100 that produces hydrogen by decomposing gaseous ammonia, and
A hydrogen fuel cell unit (200) generating electricity using the hydrogen produced by the hydrogen production unit (100)
including,
The hydrogen production unit 100 is
An ammonia decomposer 110 for thermally decomposing the gaseous ammonia, and
A method for raising the temperature of the mixed gas by exchanging heat with the mixed gas including undecomposed ammonia, hydrogen, and nitrogen discharged from the ammonia decomposer 110 with the first exhaust gas EG1 generated from the hydrogen fuel cell unit 200 1 including a heat exchanger 171,
The hydrogen fuel cell unit 200 is
A fuel cell unit 210 that passes through the first heat exchanger 171 and generates power using the hydrogen contained in the mixed gas whose temperature has been raised as fuel;
A compressor 220 pressurizing air and supplying it to the fuel cell unit 210, and
The air pressurized by the compressor 220 is heat-exchanged with the second exhaust gas EG2 generated from the fuel cell unit 210 to supply the high-temperature and high-pressure air to the fuel cell unit 210. Including a heat exchanger 230,
The hydrogen production unit 100 is
A combustor 180 generating third exhaust gas EG3 by combusting the first exhaust gas EG1 passing through the first heat exchanger 171;
The third exhaust gas (EG3) is supplied to the ammonia decomposer (110) and heat exchanged, the fuel cell power generation system. According to claim 1,
The fuel cell power generation system, wherein the first exhaust gas (EG1) passing through the first heat exchanger (171) is branched at a first branching point (10) and joined to the front end (20) of the first heat exchanger. According to claim 1,
A fuel cell power generation system further comprising a heater at the front or rear of the first heat exchanger (171). delete delete delete According to claim 1,
The hydrogen production unit 100 is
An ammonia storage tank 160 for storing liquid ammonia, and
Further comprising a vaporizer 150 for vaporizing the liquid ammonia and supplying it to the ammonia decomposer 110,
The third exhaust gas (EG3) passing through the ammonia decomposer (110) is supplied to the vaporizer (150) to exchange heat. According to claim 1,
The hydrogen production unit 100 is
Further comprising an ammonia adsorber 120 adsorbing the undecomposed ammonia in the mixed gas discharged from the ammonia decomposer 110. According to claim 8,
The ammonia adsorber 120 is a heating alternating adsorber,
A first tube 331 and a second tube 332 spaced apart from each other,
A first tube 333 connected to the inside of each of the first tube 331 and the second tube 332, and
A fuel cell power generation system comprising a second tube 334 connected to or connected to an outer surface of each of the first tube 331 and the second tube 332 to enable heat exchange. According to claim 9,
The first tube 331 and the second tube 332 are the mixed gas alternately introduced into the first tube 331 and the second tube 332 through the first tube 333. Adsorbing the undecomposed ammonia in
The first tube 331 and the second tube 332 contact or are connected to the outer surfaces of the first tube 331 and the second tube 332 through the second tube tube 334, so that the A fuel cell power generation system that is regenerated by heat exchange with mixed gas alternately. According to claim 9,
The second tube 334 includes a front-end second tube 3341 connected to the ammonia decomposer 110 and a rear-end second tube 3342 connected to the third heat exchanger 130, Fuel cell power generation system. According to claim 11,
The mixed gas supplied from the ammonia decomposer 110 to the ammonia adsorber 120 through the front end second tube 3341 exchanges heat with the first tube 331 or the second tube 332 to A fuel cell power generation system in which the first tube 331 or the second tube 332 is regenerated and supplied to the third heat exchanger 130 through the second tube 3342 at the rear end. According to claim 12,
The fuel cell power generation system, wherein the mixed gas supplied to the third heat exchanger (130) through the second rear end tube (3342) is cooled in the third heat exchanger (130). According to claim 13,
The first tube tube 333 includes a front end first tube tube 3331 connected to the third heat exchanger 130,
The mixed gas discharged from the third heat exchanger 130 is supplied into the first tube 331 or the second tube 332 through the front end first tube 3331, and the first tube ( 331) or the second tube 332, wherein the undecomposed ammonia is adsorbed. 15. The method of claim 14,
The first tube tube 333 further includes a rear end first tube tube 3332 connected to the first heat exchanger 171,
The hydrogen and nitrogen included in the mixed gas are supplied to the first heat exchanger 171 through the first tube 3332 at the rear end and exchange heat with the first exhaust gas EG1. . Any of claims 1, 2, 3, 7, 8, 9, 10, 11, 12, 13, 14, or 15 A ship equipped with the fuel cell power generation system according to paragraph 1. 17. The method of claim 16,
The ship is an ammonia carrier or an ammonia fuel propulsion ship.

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