KR101755379B1 - Fuel reforming system for submarine - Google Patents

Abstract

The present invention relates to a fuel cell; A plurality of steam fuel reformers arranged in a multi-stage and reacting methanol and water vapor by a catalyst to produce a reformed gas to be supplied to the fuel cell; A hydrogen filter for passing only hydrogen from the reformed gas discharged from the plurality of steam reformers to the fuel cell; And a reforming gas which is disposed in a multi-stage and which can not pass through the hydrogen filter using the catalyst, or a residual reforming gas that has not passed through the hydrogen filter, or a reforming gas remaining in the fuel cell and an oxidant, Wherein the fuel reformer is operated at a pressure equal to or higher than an operating pressure of the hydrogen filter. Accordingly, even when the capacity of the steam reformer is increased, efficient heat supply to the steam reformer can be performed, and the thermal distribution of the entire catalyst can be uniformly maintained.

Description

FUEL REFORMING SYSTEM FOR SUBMARINE

And more particularly, to a fuel reforming system for a submarine that generates hydrogen gas to be supplied to a fuel cell.

Generally, a submarine is classified into a diesel engine electric propulsion system and a nuclear power system as a power source. Here, a submarine powered by a diesel engine electric propulsion system is submerged using energy stored in a secondary battery such as a lead-acid battery during underwater navigation.

Therefore, when the energy of the rechargeable battery is exhausted during the submergence, the rechargeable rechargeable battery is floated to the sea surface and the rechargeable battery is recharged with the diesel engine.

The snorkeling of these submarines causes a problem of hindering the maximum concealment of the submarine, so a system called Air Independent Propulsion (AIP) is used to minimize the snorkeling period and increase the diving time.

Generally, air-borne propulsion systems for submarines include fuel cells, closed-loop diesel engines, and Stirling engines. The dual fuel cell system is an energy conversion device that directly converts chemical energy into electrical energy by electrochemical reaction of hydrogen and oxygen and is evaluated as the most suitable air-driven propulsion system for submarines.

The fuel cell system used in the submarine air-borne propulsion system uses a steam fuel reformer that stores liquid fuel in the vessel and reforms it as necessary to produce hydrogen to supply hydrogen required for electrical energy generation. The submarine fuel reformer causes steam reforming of the fuel and steam together with the catalyst to produce a reformed gas containing a large amount of hydrogen gas. The basic reaction formula is as follows.

CH ₃ OH + 2H ₂ O → 4H ₂ + CO ₂

_{CH 3 OH + H 2 O →} 3H 2 + CO

Among the reformed gases generated in the submarine reformer, hydrogen gas is supplied to the fuel cell. In this case, since the fuel and steam in the steam reformer react endothermically, it is necessary to supply heat from the outside.

On the other hand, a submarine reformer system includes a combustor that generates combustion heat to provide heat to the reformer.

In order to increase the output of the fuel cell, a large amount of hydrogen is required, and a large amount of hydrogen is required, so that the reformer capacity is increased and a lot of combustion heat must be supplied to the reformer.

However, in the prior art, when the capacity of the unit fuel reformer is increased, the heat distribution of the catalyst in one fuel reformer is not uniform, so that the reforming performance can be reduced. That is, if a reactant causes a catalytic reaction in a fuel reformer with a single package, the temperature of the reformer gradually decreases due to the endothermic reaction as the flow passes. In order to prevent this, it is necessary to supply heat from the outside to the inside of the fuel reformer. However, when the unit fuel reformer has a high capacity, it is impossible to supply heat into the unit fuel reformer.

Further, when the fuel reformer is operated with a large-sized fuel reformer in one package, there is a limitation in supplying heat recovered from the system to the fuel reformer.

Therefore, it is an object of the present invention to provide a fuel reforming apparatus capable of maintaining the entire reforming efficiency at a high efficiency state by keeping the operating temperature of the catalyst constant even when the capacity of the unit fuel reformer is increased, A submersible fuel reforming system for a submarine.

It is another object of the present invention is to provide a fuel reforming system for a submarine capable of discharging the carbon dioxide to remove the carbon contained in the fuel methanol to convert the final exhaust gas to the maximum CO _2.

In order to accomplish the above object, according to the present invention, there is provided a fuel reforming system for a submarine, comprising: a fuel cell; A plurality of steam fuel reformers arranged in a multi-stage and reacting methanol and water vapor by a catalyst to produce a reformed gas to be supplied to the fuel cell; A hydrogen filter for passing only hydrogen from the reformed gas discharged from the plurality of steam reformers to the fuel cell; And a reforming gas which is disposed in a multi-stage and which can not pass through the hydrogen filter using the catalyst, or a residual reforming gas that has not passed through the hydrogen filter, or a reforming gas remaining in the fuel cell and an oxidant, And the fuel reformer is operated at a pressure equal to or higher than the hydraulic pressure corresponding to the working pressure of the hydrogen filter and the submergence depth (depth of operation of the submarine).

According to an embodiment of the present invention, the reformed gas discharged from any one of the plurality of reformers is sequentially supplied to and discharged from another reformer, and each of the plurality of combustors is connected to an inlet of each of the plurality of fuel reformers And the temperature of the inlet of each of the plurality of fuel reformers is controlled by supplying heat so that the catalytic reaction can be smoothly performed within a plurality of fuel reformers.

According to an embodiment of the present invention, each of the plurality of steam reformers causes a reforming reaction with respect to some of the reactants. When a high-capacity fuel reformer is required, the catalytic reaction is separately generated by designing and manufacturing the fuel reformer by separating it into a plurality of fuel reformers. When the capacities of the plurality of fuel reformers are all combined, the capacity of the reformer is made equal to the capacity of the high capacity fuel reformer.

According to one embodiment of the present invention, the amount of the catalyst contained in each of the plurality of (N) steam reformer units is set such that the total amount (B) of the catalyst required for reforming the total fuel amount (A) (B / N) divided by the number of fuel reformers, and in each reformer, the catalytic reaction process can be performed only by the amount of fuel A / N divided by the total number of fuel reformers.

According to an embodiment of the present invention, the continuous reforming reaction of the plurality of steam reformers and the combustion heat of the plurality of combustors may be performed until the reforming reaction is terminated.

According to one embodiment of the present invention, the plurality of combustors controls the supply amount of the oxidizer (air or oxygen) so that the reformed gas supplied to the plurality of steam reformers reaches the target temperature of the predetermined reformer, It is possible to provide combustion heat to the gas.

According to an embodiment of the present invention, the heat generated in the plurality of combustors may be transferred to the reformed gas through the heat exchanger and the heating medium (saturated water vapor).

According to an embodiment of the present invention, the plurality of combustors are installed until the composition of the final exhaust gas discharged from the combustor disposed at the rearmost end becomes CO ₂ or H ₂ O, so that the carbon contained in the methanol is mostly CO ₂ < / RTI >

According to the present invention configured as described above, the following effects can be obtained.

First, when the unit fuel reformer becomes high capacity, a plurality of fuel reformers are divided into a plurality of units and a plurality of fuel reformers are arranged in multiple stages. In the first fuel reformer (first reformer), the endothermic reaction When the temperature falls, the temperature of the reformed gas is increased to the target temperature by using the heat recovered through the combustion reaction of the combustor, and then supplied to the second fuel reformer (second reformer). In the second reformer, The temperature of the reforming gas of the N-th fuel reformer (the N-th stage reformer) is increased by supplying heat from the combustor again. Thus, even if the capacity of the reformer is increased, efficient heat supply to the interior of the reformer is possible The thermal distribution of the whole catalyst can be maintained uniformly.

Second, carbon monoxide can not be completely removed by using only one conventional combustor. However, carbon monoxide can be removed by burning several times by using a multi-stage combustor according to the present invention, thereby discharging carbon dioxide during submergence.

1 is a conceptual diagram showing a fuel reforming system for a submarine according to the present invention.
2 is a temperature graph for explaining the temperature according to the fuel reforming system of FIG.

Hereinafter, a submarine reforming system according to the present invention will be described in detail with reference to the drawings. The singular expressions include plural expressions unless the context clearly dictates otherwise.

In the following description of the embodiments of the present invention, a detailed description of related arts will be omitted when it is determined that the gist of the embodiments disclosed herein may be obscured.

FIG. 1 is a conceptual diagram showing a fuel reforming system for a submarine according to the present invention, and FIG. 2 is a temperature graph for explaining a temperature according to the fuel reforming system of FIG.

The fuel reforming system for a submarine according to the present invention includes a plurality of steam reformers (41, 42, 43) (hereinafter abbreviated as a reformer) and a plurality of combustors (51, 52, 53, 54).

The plurality of reformers 41, 42, and 43 are arranged in multiple stages to generate a reformed gas to be supplied to the fuel cell 80. The plurality of reformers 41, 42, and 43 may be composed of a first stage reformer 41 to an Nth stage reformer connected in series to each other.

The plurality of combustors 51, 52, 53, and 54 are disposed in multiple stages to generate combustion heat for heating reactants or reformed gas flowing into each reformer 40. The plurality of combustors 50 may be a catalytic combustion burner and may be composed of the first stage combustor 51 to the Nth stage combustor.

In the N-th stage, N is a natural number of 2 or more, and the reformer shown in Fig. 1 is composed of first to third reformers 41, 42, 43, and the combustor 50 is a first- 52, 53, and 54, respectively. However, the number of reformers and combustors is not limited thereto.

The fourth stage combustor 54 is provided at the end of the plurality of combustors 51, 52, 53, and 54, and further combusts fuel (methanol) to supply insufficient heat when a heat imbalance occurs in the fuel reforming system have.

The fuel reforming system may include a plurality of fuel supply units 10 and a water supply unit 20.

The plurality of fuel supply units 10 may be arranged corresponding to the multi-stage reformer 40, respectively, and may supply fuel to the multi-stage reformer 40, respectively. The fuel supply unit 10 can supply fuel such as methanol or ethanol. Each fuel supply unit 10 is connected to the reformer 40 by a fuel supply pipe and a fuel supply pump is provided at the front end or the rear end of the fuel supply unit so that fuel having a predetermined pressure or more can be supplied to the reformer 40. A flow control valve is installed in the fuel supply pipe to adjust the fuel supply amount.

The water supply unit 20 is connected to the first-stage reformer 41 by a water supply pipe, and can supply water to the first-stage reformer 41. A water supply valve is installed in the water supply pipe, and the water supply amount can be adjusted.

The fuel reforming system may include a plurality of oxygen supply units (31, 32, 33, 34). The plurality of oxygen supply units 31, 32, 33, and 34 are disposed so as to correspond to the multi-stage combustor 50 so that oxygen is supplied to the multi-stage combustor 50 so that the combustion reaction of the reformed gas and oxygen in the combustor 50 .

The fuel reforming system may include a plurality of heat exchangers (61, 62, 63, 64, 65). The plurality of heat exchangers 61, 62, 63, 64, and 65 are disposed corresponding to the multi-stage combustor 50 and the multi-stage reformer 40 to heat the heat generated by the multi- .

Each of the plurality of heat exchangers (61, 62, 63, 64, 65) comprises first heat exchangers (61a, 62a, 63a) for providing combustion heat and second heat exchangers (61b, 62b, 63b) . The heat of combustion is transferred from the first heat exchanger (61a, 62a, 63a) to the second heat exchanger (61b, 62b, 63b). The method of transferring heat from the first heat exchangers 61b, 62b, 63b to the second heat exchangers 61b, 62b, 63b can be either a direct heat transfer method or an indirect heat transfer method.

In the direct heat transfer system, the combustor 50 is installed around the catalytic reactor of the reformer 40 so that the combustion heat is directly supplied to the catalytic reactor. This method has the advantage that the steam reformer 40 can be downsized because the heat of the combustion burner can be directly transferred in the vicinity of the catalytic reactor.

The indirect heat transfer system forms a circulation flow path through which the heat transfer fluid circulates between the first heat exchanger (61a, 62a, 63a) and the second heat exchanger (61b, 62b, 63b), and the heat of combustion is heat exchanged through the heat transfer fluid 62a, 63a to the second heat exchangers 61b, 62b, 63b through the heating medium (saturated water vapor). At this time, the heat of combustion is transferred to the heat transfer fluid through the first heat exchanger 61a, 62a, 63a, and the heat medium moves to the second heat exchanger 61b, 62b, 63b along the circulation flow path to the second heat exchanger 61b 62b, and 63b to heat exchange with the reformed gas discharged from the reformer 40, thereby transferring heat to the reformed gas.

Each of the plurality of reformers 41, 42 and 43 is supplied with fuel and water from the plurality of fuel supply units 10 and the water supply unit 20 as reactants and is supplied to the reformer 40 ) To generate a reformed gas containing hydrogen, carbon dioxide, and carbon monoxide.

The plurality of reformers are operated at a high pressure. The plurality of reformers can be operated at a high pressure due to the supply of methanol over a predetermined pressure from the fuel supply unit and the vaporization of water vapor. For example, the operating pressures of a plurality of reformers must overcome not only the operating pressure of the hydrogen filter but also the water pressure according to the operating depth of the submarine (depth of submergence) so that the reformed gas can pass through the hydrogen filter. Therefore, the plurality of reformers are operated at a pressure equal to or higher than the hydraulic pressure of the hydrogen filter and the hydraulic pressure (1 atmospheric pressure increase per 10 m of depth) depending on the depth of the submerged fuel, and the high- The reformed gas is supplied to the fuel cell through the hydrogen filter, and the carbon in the residual exhaust gas can be converted to carbon dioxide to discharge carbon dioxide during the submergence.

Here, each of the plurality of reformers 41, 42, and 43 does not perform steam reforming for all reactants, but steam reforming is performed only with some of the reactants of all the reactants. Steam reforming can be achieved only with some reactants in the total reactants by the following three methods.

First, it reduces the amount of catalyst and the reaction time of the catalyst. The amount of the reforming gas produced by the steam reforming reaction is proportional to the amount of the catalyst and the reaction time of the catalyst. Therefore, as the amount of the catalyst is reduced or the reaction time of the catalyst is shortened, the reforming gas produced by the reaction with the catalyst decreases. For example, reactants can catalyze all reactants if they give enough time to catalyze. However, if the time to catalyze is reduced, only a part of the reactants will react.

The catalyst contained in each of the first to Nth reformers (41, 42, 43) of the present invention may be embedded in a reduced ratio to the total amount of the catalyst. The amount of the catalyst can be adjusted depending on the number of the reformers 40. In addition, since the size of the reformer 40 in which the catalyst is incorporated is limited, the time for reactants to react with the catalyst can be reduced as the catalyst incorporated in the reformer 40 is reduced.

For example, suppose that the amount of catalyst B is needed to reform a positive fuel A, and if there are four fuel reformers, the amount of catalyst entering each fuel reformer is reduced by B / 4. Thereby, in the first fuel reformer, the catalytic reaction is performed by the amount of A / 4 fuel.

Second, it is a method to control the ratio of reactants. That is, if the ratio of the fuel (methanol) and water supplied to each of the first to Nth reformers 41, 42 and 43 is adjusted, only a part of methanol can be reacted.

Third, the temperature of the reformer is controlled. By controlling the inlet temperatures of the first to Nth reformers, only a part of the fuel amount of the total fuel amount can be catalytically treated in each reformer.

The fuel reforming system may include a steam generating heat exchanger (64b, 65b) for heating and vaporizing the water discharged from the water supplying section (20).

The fuel reforming system may include a plurality of heat recovery heat exchangers (64a, 65a). The plurality of heat recovery heat exchangers 64a and 65a are installed at a rear stage of the Nth stage combustor 54 and a part of the plurality of heat recovery heat exchangers 64a and 65a is discharged from the Nth stage combustor 54 A part of the heat of combustion can be recovered and the heat can be transferred to the steam generating heat exchangers 64b and 65b.

Another part of the plurality of heat recovery heat exchangers 64a and 65a may be used to recover the other part of the combustion heat emitted from the Nth stage combustor 50 and to heat the fuel discharged from the fuel supply part 10. [ have. To this end, a fuel heating heat exchanger 65c is provided in the fuel supply pipe, and the fuel heating heat exchanger 65c can receive heat from the heat recovery heat exchanger 65a to heat the fuel.

The heat recovered through the heat exchanging heat exchanger 65c can be heat-transferred by a direct heat transfer method or an indirect heat transfer method.

Hereinafter, the operation of the fuel reforming system for a submarine according to the present invention will be described.

Since it is difficult to reform the fuel amount A, which is a reactant of the fuel reforming system, at once, the amount of fuel A is divided by A / N and injected into the inlet of each reformer. At this time, the amount of the catalyst corresponding to (A / N) in the amount of injected fuel of each reformer is included in each reformer.

In this embodiment, three reformers are continuously arranged in multiple stages, and methanol of A / 3 is supplied from the first to third fuel supply units 10 to the inlet of the first to third reformers 41, Respectively. In addition, the water is discharged from the water supply unit 20, vaporized by steam, and then sequentially supplied to the first to third reformers 41, 42, and 43.

At this time, the fuel (methanol) supplied from the first to third fuel supply units 11, 12, and 13 can be heated by receiving heat from the heat exchanger 65c. The heat exchanger 65c receives heat from a heat exchanger 65a installed at the rear end of the hydrogen filter. At this time, the heat transfer between the heat exchangers installed before and after the hydrogen filter 70 can be performed through the heating medium (saturated water vapor). The heat exchanger 65a acquires the heat generated in the combustor 54. [

Similarly, the water supplied from the water supply unit 20 acquires heat from the heat exchangers 64b and 65b and is vaporized by water vapor, and the vaporized water vapor can be raised to a set temperature, for example, 250 to 300 degrees Celsius. The heat exchangers 64b and 65b receive heat from the heat exchangers 65a and 64a installed after the hydrogen filter 70. [ At this time, heat can be transferred between the two heat exchangers through the heating medium (saturated steam). The heat exchangers (65a, 64a) receive heat from the combustor (54).

Methanol and water vapor supplied to the first-stage reformer 41 receive heat generated by the third stage combustor 53 through the heat exchanger 61a and the heat exchanger 61b and are heated to a target temperature. The first stage reformer 41 reacts methanol and steam with a steam reforming reaction to produce a reformed gas containing hydrogen. The first stage reformer 41 is configured to reform only a part of the entire reactants. Some reforming of the first-stage reformer 41 may be achieved by adjusting the amount of fuel supplied or the amount of catalyst contained therein (catalyst reaction time).

At the downstream of the first-stage reformer 41, hydrogen, carbon monoxide, carbon dioxide, water vapor, and fuel that are not involved in the reforming reaction are present in the reforming reaction. The temperature of the reformed gas and the residual fuel at the downstream of the first-stage reformer 41 decreases to 300 degrees or less due to the endothermic reaction. The reformed gas and the fuel again receive the combustion heat from the second stage combustor 52, rise again to the target temperature, and are supplied to the second stage reformer 42.

The second stage reformer 42 is connected to the downstream end of the first stage reformer 41 and receives hydrogen, carbon monoxide, carbon dioxide, steam, and fuel not participating in the reforming reaction from the first stage reformer 41, To generate reformed gas.

The second-stage reformer 42 is also designed to reform only a part of the residual fuel, not designed to be large-sized so as to perform the reforming reaction on all of the remaining fuel. The multistage reformer 40 is a continuous process until the fuel supplied to the first-stage reformer 41 is converted into a reformed gas usable in the fuel cell 80. That is, the reforming reaction of the multi-stage reformer 40 is continuously performed until the residual fuel that can be reformed is eliminated.

The multi-stage reformer 40 according to the present embodiment is composed of first to third reformers 41, 42 and 43, and the whole reactant passes through the third stage reformer 43 from the first stage reformer 41 While the reforming of the fuel is completed.

Hydrogen, carbon monoxide and carbon dioxide are mainly generated as the reforming gas generated by the reforming reaction in the multi-stage reformer 40. The hydrogen filter 70 provided at the rear stage of the third stage reformer 43 passes only hydrogen in the reformed gas and the hydrogen which has been passed is supplied to the fuel cell 80 to generate electric energy in the fuel cell 80 do.

The remaining reforming gas discharged from the hydrogen filter 70 is also composed of residual hydrogen, carbon monoxide, and carbon dioxide. In the submarine, all of the reformed gas must be converted to carbon dioxide, so that the remaining reformed gas is sequentially supplied to the first stage to third stage combustors 51, 52, 53 connected to the rear end of the hydrogen filter 70 and is all burned to convert carbon monoxide into carbon dioxide do.

The remaining reformed gas is combusted by the first to third combustors 51, 52 and 53, and the combustion heat secured through the combustion of the remaining reformed gas is passed through the first to third combustors 51, Through the heat exchangers (61, 62, 63) disposed at the downstream ends of the reformer (41, 423).

For example, each of the plurality of combustors 51, 52, 53, and 54 may be disposed in multiple stages between a plurality of reformers 41, 42, and 43 arranged in multiple stages. Or a plurality of heat exchangers 61b, 62b, and 63b that are thermally transferred from the plurality of combustors 51, 52, 53, and 54 may be disposed in multiple stages between the plurality of reformers 41, 42, and 43.

When the target temperatures of the plurality of reformers 41, 42, and 43 arranged in multiple stages are set, the plurality of combustors 51 and 52 arranged in multiple stages so that the temperature of the reformed gas supplied to each reformer 40 becomes the target temperature , 53, 54).

The continuous reforming reaction of the plurality of reformers 41, 42, 43 arranged in multiple stages and the furnace heat supply of the plurality of combustors 51, 52, 53, 54 arranged in multiple stages are performed until the reforming reaction is completed.

The fuel reforming system for a submarine according to an embodiment of the present invention uses a methanol fuel reformer (40).

The fuel reforming system for a submarine according to the present invention is constituted by dividing the capacity of the reformer (40) into multiple stages.

Hereinafter, the temperature changes of the reactant and the reformed gas will be described with reference to FIG.

In the fuel reforming system for a submarine according to the present invention, the inlet temperature (temperature of methanol and water vapor) of the fuel reformer at each stage can be set to a target temperature of 250 to 300 degrees. In this embodiment, the combustion heat recovered from the first to fourth combustors 51, 52, 53, and 54 can be recovered and used to heat the gas flowing into the fuel reformer to 250 to 300 degrees.

The temperature of the water vapor supplied to the first-stage reformer 41 can be lowered by the introduction of methanol.

The reformed gas discharged from the first-stage reformer 41 becomes lower than the target temperature in accordance with the endothermic reaction.

For example, the inlet temperature of the first-stage reformer (41) is raised to the target temperature by the combustion heat of the multi-stage combustor (50). The reformed gas generated from the second-stage reformer 42 will be lower than the target temperature. However, as the steam amount of the second-stage reformer 42 is reduced compared to the steam amount of the first-stage reformer 41, ) Of the reforming gas.

The temperature of the reformed gas discharged from the second-stage reformer 42 is again raised to the target temperature by using the multi-stage combustor 50.

This process is continuously carried out until the reforming reaction no longer occurs due to the heat of combustion provided from the multi-stage combustor 50. The carbon monoxide contained in the residual reforming gas that has passed through the multi-stage combustor 50 is burned by the multi-stage combustor 50 to be converted into carbon dioxide, and the converted carbon dioxide can be discharged to the seawater.

It will be apparent to those skilled in the art that various modifications, substitutions and alterations can be made hereto without departing from the spirit and scope of the invention as defined by the appended claims. will be.

It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory and are intended to provide further explanation of the invention as claimed. .

The scope of protection of the present invention should be construed according to the following claims, and all technical ideas within the scope of equivalents should be interpreted as being included in the scope of the present invention.

10: fuel supply unit
11: First fuel supply part
12: Second fuel supply part
13: Third fuel supply part
14: Fourth fuel supply part
20: water supply part
30: oxygen supply section
31: First oxygen supply unit
32: second oxygen supply part
33: Third oxygen supply unit
34: fourth oxygen supply unit
40: reformer
41: First stage reformer
42: Second stage reformer
43: Third stage reformer
50: Combustor
51: First stage combustor
52: Second stage combustor
53: Third stage combustor
54: Fourth stage combustor
60: heat exchanger
70: Hydrogen filter
80: Fuel cell

Claims (8)

A fuel cell provided inside the submarine;
A plurality of steam fuel reformers connected in series and arranged in a plurality of stages to generate a reformed gas to be supplied to the fuel cell by reacting methanol and steam with a catalyst;
A hydrogen filter for passing only hydrogen from the reformed gas discharged from the plurality of steam reformers to the fuel cell;
A reforming gas introduced into the plurality of steam reformers, which is connected in series and is arranged in a plurality of stages, causes a combustion reaction between the residual reforming gas that has not passed through the hydrogen filter using the catalyst or the reforming gas remaining in the fuel cell, A plurality of combustors for supplying heat to the combustion chamber; And
A plurality of heat exchangers connected to the plurality of steam reformers and corresponding to the plurality of combustors, respectively;
Lt; / RTI >
Wherein all of the reformed gas discharged from any one of the plurality of steam reformers is supplied to the other steam reformer,
Wherein the plurality of combustors exhaust heat from one of the steam reformers to supply combustion heat to the reformed gas supplied to the other steam reformer,
Heat generated from any one of the plurality of combustors is transferred to the reformed gas through the heat exchanger,
Wherein the plurality of steam reformers operate at a pressure equal to or higher than a hydraulic pressure corresponding to an operating pressure of the hydrogen filter and an operating depth of the submarine. delete The method according to claim 1,
Wherein each of the plurality of steam reformers causes a reforming reaction with respect to a part of reactants of all the reactants. The method of claim 3,
Wherein the plurality of steam reformers adjust the amount of fuel supplied from the fuel supply unit or adjust the amount of the catalyst installed therein, the reaction time of the catalyst, or the temperature of the reformer to cause a reforming reaction with the reactants of the part Fuel reforming system for submarines. The method according to claim 1,
Wherein the continuous reforming reaction of the plurality of steam reformers and the combustion heat supply of the plurality of combustors are performed until the reforming reaction is terminated. 6. The method of claim 5,
Wherein the plurality of combustors controls the supply amount of the oxidizing agent (air or oxygen) so that the reformed gas supplied to the plurality of steam reformers reaches the target temperature of the predetermined reformer, thereby providing the combustion heat to the reformed gas Fuel reforming system for submarines. delete The method according to claim 1,
Wherein the plurality of combustors are provided until the composition of the final exhaust gas discharged from the combustor disposed at the rearmost end becomes CO ₂ or H ₂ O so that the carbon contained in methanol is converted to CO ₂ system.

Images