KR101696550B1 - Ship - Google Patents

Abstract

The present invention relates to a vessel comprising: a raw material supply part for supplying raw materials; a raw material water supply part for supplying raw material water; a fuel cell system generating electricity using the raw material supplied from the raw material supply part and the raw material water supplied from the raw material water supply part; and an electricity conversion part converting direct current (DC) output from the fuel cell system into alternating current (AC).

Description

Ship {SHIP}

The present invention relates to an environmentally friendly vessel.

In general, most of the total energy comes from fossil fuels. However, the reserves of fossil fuels are limited, and the use of fossil fuels has serious effects on the environment such as air pollution, acid rain, and global warming. Environmentally friendly power generation systems have been developed to solve the problems associated with the use of such fossil fuels.

Environmentally friendly power generation systems include power generation systems that produce electricity by converting renewable energy, including sunlight, water, geothermal, precipitation, and bio-organisms. An environmentally friendly power generation system also includes a power generation system that converts fossil fuels or produces electricity through chemical reactions such as hydrogen and oxygen.

A fuel cell system is a system that includes a fuel cell (FUEL CELL) that directly produces electrical energy through reaction with an oxidizing agent such as oxygen using, for example, hydrogen contained in a hydrocarbon-based material. Substance hydrocarbons include, for example, NG (natural gas), LPG (liquefied petroleum gas), methanol (CH ₃ OH), ethanol (C ₂ H ₅ OH), petrol, dimethyl ether and the like.

Alkaline fuel cell (AFC), phosphoric acid fuel cell (PAFC), molten carbonate fuel cell (MCFC), solid oxide fuel cell (MCFC), and solid oxide fuel cell (SOFC), a polymer electrolyte membrane fuel cell (PEMFC), and a direct methanol fuel cell (DMFC). Each of these fuel cells operates on essentially the same principle, but the operating temperature, electrolyte, power generation efficiency, and power generation performance are different.

A conventional fuel cell system vaporizes LNG using a separate heating device to supply hydrogen to the fuel cell. Accordingly, the conventional fuel cell system has the following problems.

First, the conventional fuel cell system needs to supply fuel or electricity to the heating device to vaporize the LNG. Accordingly, the fuel cell system according to the related art has a problem in that the fuel cell and the heating device use the fuel separately or supply electricity from the outside, thereby lowering the electricity production amount and the electricity production efficiency.

Second, the fuel cell system according to the related art requires a separate heating device for vaporizing the LNG, which increases the installation cost of the heating device. Accordingly, the fuel cell system according to the related art has a problem that the construction cost for producing electricity is increased.

Third, the fuel cell system according to the prior art requires a space for installing a heater for vaporizing the LNG. Therefore, the fuel cell system according to the related art has a problem that the space of other devices for generating and storing electricity due to the installation of the heating device becomes narrow.

SUMMARY OF THE INVENTION The present invention has been made to solve the above-mentioned problems, and it is an object of the present invention to provide a ship capable of reducing the installation cost and increasing the space utilization for the installation space.

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In order to solve the above-described problems, the present invention can include the following configuration.

A ship according to the present invention comprises a raw material supply part for supplying a raw material; A raw water supply part for supplying raw water; A fuel cell system for generating electricity using raw material supplied from the raw material supply unit and raw material water supplied from the raw water supply unit; And a power conversion unit for converting a direct current (DC) output from the fuel cell system into an alternating current (AC), wherein the fuel cell system includes a raw material processing unit for pre-processing a raw material supplied from the raw material supply unit, A reformer for reforming steam (H ₂ 0) supplied from the raw water treatment section supplied from the raw material treatment section, and a combustor for heating the reformer A hydrogen generating part including the hydrogen generating part; A fuel cell that generates electricity using fuel including hydrogen supplied from the hydrogen generator; And a first heat exchanger for exchanging heat between the steam (H ₂ 0) supplied from the raw water water processor and the exhaust gas discharged from the combustor. The steam (H ₂ 0) passed through the first heat exchanger is supplied to the raw material processor And can be used as a heat source for vaporizing the fuel.
Ship in accordance with the present invention, the raw material processing via steam that (H ₂ 0) to heat comprise a second heat exchange unit for heat exchange with steam (H ₂ 0) passed through the exhaust gas and the material processing unit to be discharged from the fuel cell .
A ship according to the present invention includes: an air supply unit for supplying air to the fuel cell; And a third heat exchanger for exchanging heat between the exhaust gas passing through the first heat exchanger and the air supplied to the fuel cell so that the air supplied from the air supplier to the fuel cell is heated.
In the vessel according to the present invention, the raw water treatment section may include a water separator for separating moisture from steam (H ₂ 0); An economizer for generating steam (H ₂ 0) supplied to the raw material treatment unit and the water separator by using exhaust gas discharged from a gas engine that generates propulsion force as fuel containing hydrogen generated in the raw material treatment unit; And a circulation unit for circulating the fluid between the water separator and the economizer to recover heat from the exhaust gas discharged from the gas engine.

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According to the present invention, the following effects can be achieved.

The present invention can be implemented to vaporize LNG with the waste heat of the exhaust gas generated in the fuel cell, thereby improving the electricity production amount and the electricity production efficiency.

The present invention is implemented to vaporize LNG with the waste heat of the exhaust gas generated in the fuel cell, thereby reducing the construction cost consumed in producing electricity, and it can be installed in a narrow installation space. .

1 is a conceptual diagram of an overall system according to the present invention;
2 is a conceptual diagram of a fuel cell system according to the first embodiment of the present invention
FIGS. 3A and 3B are diagrams for explaining the operation of the fuel cell used in the present invention. FIG. 3A is a conceptual diagram of a solid oxide fuel cell (SOFC)
3B is a conceptual diagram of a polymer electrolyte fuel cell (PEMFC)
4 is an exemplary diagram for explaining a hydrogen generator according to an embodiment of the present invention.
5 is a conceptual configuration diagram of a fuel cell system according to a second embodiment of the present invention
Figs. 6 and 7 are schematic diagrams of the fuel cell system according to the first embodiment of the fuel cell system of Fig. 5
Fig. 8 is a schematic view of the fuel cell system of Fig. 5 according to the second embodiment
Fig. 9 is a schematic view of the fuel cell system of Fig. 5 according to the third embodiment
Fig. 10 is a schematic view of the fuel cell system of Fig. 5 according to the fourth embodiment
11 is a schematic view showing an example of a ship according to the present invention

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

FIG. 2 is a conceptual diagram of a fuel cell system according to a first embodiment of the present invention. FIGS. 3A and 3B are views showing the structure of a fuel cell used in the present invention. Fig. 3 is a conceptual diagram of a solid oxide fuel cell (SOFC), Fig. 3 (b) is a conceptual diagram of a polymer electrolyte fuel cell (PEMFC) FIG. 2 is a diagram illustrating an example of a hydrogen generating portion according to the present invention.

Referring to FIG. 1, a fuel cell system 200 according to the present invention is applied to a power generation system 100 to perform a function of generating electricity. Before describing the fuel cell system 200 according to the present invention, the power generation system 100 will be described first.

The power generation system 100 includes a raw material supply unit 110, a raw water supply unit 120, an air supply unit 130, a power conversion unit 140, and a fuel cell system 200 according to the present invention.

The raw material supply unit 110 includes a raw material storage tank and supplies the raw material from the raw material storage tank. For example, the raw material is a material of a hydrocarbon series, NG (natural gas), LPG (liquefied petroleum gas), methanol (CH ₃ OH), ethanol (C ₂ H ₅ OH), petrol, dimethyl ether, methane, hydrogen Purified off-gas, pure oxygen, and the like.

For example, when the power generation system 100 is applied to an automobile, the raw material supply unit 110 is implemented including a gas storage tank and a device (for example, a pump) for supplying gas from the gas storage tank. As another example, when the power generation system 100 is applied to an LNG carrier, the material supply unit 110 is implemented including an LNG storage tank and an apparatus for providing evaporative gas generated in the LNG storage tank. As another example, when the power generation system 100 is applied to a diesel engine ship, the raw material supply unit 110 may be implemented with a diesel fuel storage tank and a device for supplying diesel fuel from the diesel fuel storage tank .

The raw water supply part 120 may include a raw water storage tank and a device (for example, a pump) for supplying raw water from the raw water storage tank. The raw water may be, for example, water (constant water), fresh water, or seawater. As another example, the raw water may be impurity-treated water or ion-removed water in fresh water or seawater.

The air supply unit 130 supplies air to the fuel cell system 200 according to the present invention. Normally, air means a gas including nitrogen, oxygen, carbon dioxide and the like, but also includes the case where all gases other than oxygen such as nitrogen or carbon dioxide, or both gases are removed from the air. The air supply unit 130 may include an air storage tank and a device (for example, a blower) for supplying air from the air storage tank. As another example, the air supply unit 130 may be configured to supply external air and compress the high-pressure air, or supply the compressed high-pressure air at normal pressure.

The power conversion unit 140 converts the direct current (DC) output from the fuel cell system 200 according to the present invention into an alternating current (AC). The power conversion unit 140 includes a DC-DC converter for boosting or reducing the output voltage from the fuel cell system 200 according to the present invention, and a DC-AC converter for converting a direct current (DC) An inverter or the like. The power conversion unit 140 discharges the electric power supplied from the fuel cell system 200 according to the present invention to the electric power load. The electric power load may be, for example, in-ship electrical equipment such as a ship's basic electrical equipment and cargo-system electrical equipment in the case of a ship. Although not shown, the power conversion unit 140 may be implemented to transmit and store electricity to an energy storage device, for example, a battery.

The fuel cell system 200 according to the present invention produces electricity using fuel, water (H ₂ O), and air. The fuel cell system 200 according to the present invention can be used in a small structure such as a home or an automobile, and can be used in a large structure such as a ship. The fuel cell system 200 according to the present invention may be implemented to operate in conjunction with a diesel engine, a gas engine, a steam turbine, a gas turbine, or a Rankine Cycle using the combustion energy of the raw material.

Hereinafter, the fuel cell system 200 according to the present invention will be described in detail with reference to the accompanying drawings.

Referring to FIG. 2, the fuel cell system 200 according to the first embodiment of the present invention includes a fuel cell 210, and a hydrogen generation unit 400. The fuel cell system 200 according to an embodiment of the present invention may be implemented by including a controller 250 for controlling all operations including the fuel cell 210 and the hydrogen generator 400 . In this specification, the raw material and the raw water, which are introduced into the hydrogen generator 400, and the fuel generated in the hydrogen generator 400 and introduced into the fuel cell 210 are defined as fuel.

The fuel cell 210 is implemented including a fuel cell stack. The fuel cell stack has an electrolyte layer formed between a cathode and an anode and a separator for supplying hydrogen and supplying air and recovering heat to the anode and the cathode And the unit cell modules are connected in series by the required number of units.

The fuel cell 210 is a temperature sensor and a device for maintaining temperature. That is, a heater, a cathode fan, and an anode fan, a cooling plate, and the like. The temperature sensor senses the temperature of the fuel cell stack, the temperature of the cathode, and the temperature of the anode. The heater can heat the fuel cell to maintain the temperature required for the operation. The air cathode fan dissipates heat generated at the cathode of the fuel cell stack. The fuel electrode fan dissipates the heat generated from the anode of the fuel cell stack. The air cathode fan and the anode cathode fan may be implemented as a part of a heat exchanger used in a fuel cell stack.

When the fuel cell system 200 according to the present invention includes the control unit 250, the control unit 250 controls the heater, the cathode fan, and the anode electrode fan using the signal output from the temperature sensor, ) Is appropriately maintained. For example, the control unit 250 maintains the operating temperature of the phosphoric acid fuel cell (PAFC) at 190 to 210 ° C, maintains the operating temperature of the MCFC at 550 to 650 ° C, In the case of oxide fuel cells (SOFC), the operating temperature is maintained at 650 to 1000 ° C. For polymer electrolyte fuel cells (PEMFC), the operating temperature is maintained at 30 to 80 ° C.

Hereinafter, the operation of the fuel cell 210 included in the fuel cell system 200 according to the present invention will be described with reference to FIGS. 3A and 3B. FIG. 3A is a conceptual configuration diagram of a solid oxide fuel cell (SOFC)), and FIG. 3B is a conceptual configuration diagram of a polymer electrolyte fuel cell (PEMFC).

3A, a solid oxide fuel cell (SOFC) 310 includes a cathode 311, an anode 313, and a cathode 313. The anode 313 is connected to the anode 312 through an electrolyte 312, . The fuel containing hydrogen (H ₂ ) flows in the anode 313 and oxygen ions (O ^{2 -} ) and hydrogen (H ₂ ) move to the anode 313 through the electrolyte 312. It reacts electrochemically with water (H ₂ O) and electron (e ^-) is generated. Since electrons are consumed in the cathode 311, electricity flows when the cathode 311 and the anode 313 are connected to each other.

The solid oxide fuel cell (SOFC) (310) is a fuel electrode (anode) (313) unreacted and electrochemical unreacted material as a the fuel carbon monoxide (CO), carbon dioxide (CO ₂₎ that may be included in the feed to hydrogen (H ₂ ) and to discharge the water (H ₂ 0 as a liquid or gaseous), such as residual material and reaction product. In addition, unreacted oxygen and nitrogen are discharged from the cathode 311 of the solid oxide fuel cell (SOFC) 310.

Referring to FIG. 3B, the PEMFC 320 includes a catalyst layer 322 formed on the anode 321, and hydrogen (H ₂ ) is generated as hydrogen ions (H ⁺ ) and electrons (e ^- do. The hydrogen ions H ⁺ move to the cathode 324 through the polymer electrolyte membrane 323. The polymer electrolyte fuel cell (PEMFC) 320 reacts with hydrogen ions (H ⁺ ) and oxygen (O ₂ ) in the catalyst layer 325 formed on the cathode 324 to produce water (H ₂ O). When the catalyst layer 322 formed on the anode 321 and the catalyst layer 325 formed on the cathode 324 are connected to each other, electricity flows.

The polymer electrolyte fuel cell (PEMFC) 320 discharges residual material such as unreacted hydrogen (H ₂ ) from the catalyst layer 322 of the anode 321. The polymer electrolyte fuel cell (PEMFC) 320 discharges unreacted oxygen and water (H ₂ O) from the cathode 324.

Other molten carbonate fuel cell (MCFC) is a fuel electrode (anode) of hydrogen (H ₂₎ and carbonate ions (CO ₃ ^2-) in the reaction water (H ₂ O) and carbon dioxide (CO _2), electron (e ^-) in the Is generated. The generated carbon dioxide (CO ₂ ) is sent to the cathode, and carbon dioxide (CO ₂ ) and oxygen (O ₂ ) react with each other at the cathode to produce carbonate ion (CO ₃ ^-2 ). Carbonate ions (CO ₃ ^-2 ) migrate through the electrolyte to the anode. In a molten carbonate fuel cell (MCFC), carbon dioxide (CO ₂ ) generated in the process of generating electricity can be implemented to be circulated in the fuel cell without being discharged to the outside.

2 and 4, the hydrogen generator 400 includes an apparatus for generating a fuel, that is, hydrogen (H ₂ ) gas, necessary for the anode of the fuel cell 210 using the raw material. In this specification, the raw material and the raw water that are introduced into the hydrogen generating unit 400 and the fuel that is generated in the hydrogen generating unit 400 and flows into the fuel cell 210 are defined as the fuel.

The hydrogen generator 400 may be designed to have various structures depending on the type of the fuel cell 210 or to improve electricity generation efficiency. For example, when the fuel cell 210 is a molten carbonate fuel cell (MCFC) or a solid oxide fuel cell (SOFC), the hydrogen generator 400 may include a reformer and a combustor . In another example, when the fuel cell 210 is a PAFC or a PEMFC, the hydrogen generator 400 may be a water gas shift reactor , ≪ / RTI > WGS).

The water gasification reactor (WGS) may be a high temperature shift reactor (HTS), a mid-temperature shift reactor (MTS), a low-temperature shift reactor (LTS) Or a carbon monoxide remover. The carbon monoxide remover may include a selective oxidation reactor (PROX) for burning and removing only carbon monoxide (CO), or a methanation reactor for reducing carbon monoxide (CO) to hydrogen (H ₂ ) .

Referring to FIG. 4, an example of the hydrogen generator 400 in the fuel cell system 200 according to an embodiment of the present invention will be described as follows.

The hydrogen generator 400 may include a raw material processing unit 410, a raw material water processing unit 420, a reformer 430, and a combustor 440.

The raw material processing unit 410 preprocesses the raw material supplied from the raw material supply unit including the raw material storage tank. For example, the raw material processing unit 410 may include an LNG evaporator for evaporating the liquefied natural gas supplied from the LNG storage tank. When the raw material is a liquid raw material having a relatively high molecular weight such as Marine Gas Oil (MGO), Marine Diesel Oil (MDO), Heavy Fuel Oil (HFO), etc., 410) including the methane flame for generating a marine gas oil (MGO), marine diesel oil (MDO), or the general fuel oil (HFO) methane by the reaction of the heated raw material and the heater applies heat the catalyst to the (CH ₄₎ Can be implemented. In addition, the raw material treatment unit 410 may include a filter for removing sulfur compounds and impurities contained in the raw material, and a desulfurizer for removing sulfide.

The raw water treatment unit 420 prepares the raw water supplied from the raw water supply unit including the raw water storage tank. The raw water water treatment unit 420 generates steam H ₂ 0 by heating the raw water and supplies the steam H ₂ 0 to a reformer. The raw water water treatment unit 420 may include a heat exchanger for heating the raw water to waste heat generated in the combustor 440, for example. The raw water water treatment unit 420 may include a steam separator for separating moisture (water droplets) contained in the exhaust gas or steam of the fuel cell system. In addition, the raw water treatment unit 420 may use activated carbon, ion removal resin, or the like to maintain the purity required for the raw material water in the fuel cell system, and may include a sensor and a control system for measuring the same. In addition, an external water supply line and a system for maintaining a predetermined level of water in the water supply unit 420 may be included.

The reformer 430 reforms the pre-treated fuel supplied from the raw material treatment unit 410 and the steam H ₂ 0 supplied from the raw water treatment unit 420 to supply hydrogen (H ₂ ) Thereby generating a reforming gas. In the reforming reaction, the reformer 430 may use thermal energy provided by the combustor 440. Hereinafter, the reforming gas from the reformer 430 is defined as fuel.

The reformer 430 is implemented with a reforming catalyst layer that triggers a reforming reaction. The reforming catalyst layer has a structure in which the reforming catalyst is packed with a catalyst supported on the carrier. The reforming catalyst is composed of nickel (Ni), ruthenium (Ru), platinum (Pt) or the like. The shape of the carrier carrying the catalyst may be, for example, granular, pellet or honeycomb, Resistant metal such as alumina (Al ₂ O ₃ ), titania (TiO ₂ ), or the like.

In the fuel cell system 200 according to the present invention, the reformer 330 may be installed outside the fuel cell 210. In this case, the fuel cell 210 is implemented as an external reforming type. In the fuel cell system 200 according to the present invention, the reformer 330 may be installed inside the fuel cell 210 in the form of a reforming catalyst layer. In this case, the fuel cell 210 is implemented as an internal reforming type.

The combustor 440 provides heat to the reformer 430 to smoothly perform the reforming reaction. When the reformer heating temperature by the combustor 440 is low, the reforming reaction by the endothermic reaction of the reformer 430 does not progress well and moisture (water droplets) is generated in the reformer 430 . If the heating temperature of the combustor 440 is high, the catalytic activity of the reforming catalyst layer of the reformer 430 may be lowered.

The combustor 440 is connected to the raw material pretreated in the raw material treatment section 410, the exhaust gas discharged from the anode of the fuel cell stack of the fuel cell 210, Can be used as the fuel. The combustor 440 may use air supplied from the air supply unit 130 (shown in FIG. 1). In the fuel cell system 200 according to the present invention, the combustor 440 may further use air discharged from the cathode of the fuel cell stack of the fuel cell 210.

Although not shown, the hydrogen generator 400 may further include at least one temperature sensor. The temperature sensor detects the temperature of the reformer 430. The temperature of the reformer (Reformer) (430) has an optimum temperature by the conditions such as the reformer (Reformer) (430) configuration, and mixing ratio of the fuel and steam (H ₂ 0) pre-treatment in the raw material processing unit 410 of the The range changes. When the fuel cell system 200 according to an embodiment of the present invention includes the control unit 250 (shown in FIG. 2), the controller 250 controls the combustor 440 The temperature of the reformer 430 is controlled by increasing or decreasing the amount of raw material combustion. For example, the controller 250 may be configured to control the temperature within a range of about ± 20 ° C. with respect to the optimum temperature range.

Here, the gas generated through the reforming reaction in the reformer 430 includes not only hydrogen (H ₂ ) but also carbon monoxide (CO), carbon dioxide (CO ₂ ), and the like. When the fuel cell 210 is a polymer electrolyte fuel cell (PEMFC), carbon monoxide (CO) poisons the electrode catalyst of the fuel cell stack of the polymer electrolyte fuel cell (PEMFC) to shorten the life of the fuel cell 210. In order to reduce the concentration of carbon monoxide (CO) to 10-20 ppm or less, the hydrogen generating unit 400 may further include a water gasification reactor (WGS) 450.

The water gasification reactor (WGS) 450 reacts with carbon monoxide (CO) and steam (H ₂ O) to produce carbon dioxide (CO ₂ ) and hydrogen (H ₂ ). The water gasification reactor (WGS) 450 may be implemented with a high temperature aqueous gasification reactor (HTS) and a low temperature aqueous gasification reactor (LTS) as shown in FIG.

The optimum temperature of the high temperature aqueous gasification reactor (HTS) and the low temperature aqueous gasification reactor (LTS) varies depending on the type of the catalyst used and the composition of the gas discharged by the equilibrium of the control temperature is determined. Although not shown in FIG. 4, a cooler and a temperature sensor may be installed in the high temperature aqueous gasification reactor (HTS) and the low temperature aqueous gasification reactor (LTS), respectively. In the case where the fuel cell system 200 according to the embodiment of the present invention includes the controller 250 (shown in FIG. 2), the controller 250 controls the cooler using the signal output from the temperature sensor, Temperature gasification reactor (HTS) and the low temperature aqueous gasification reactor (LTS). For example, the high temperature aqueous gasification reactor (HTS) is controlled within a range of 300 to 430 ° C, and the low temperature aqueous gasification reactor (LTS) is controlled within a range of 200 to 250 ° C.

Although not shown, the water gasification reactor (WGS) 450 may include a carbon monoxide remover. The carbon monoxide remover removes a very small amount of carbon monoxide (CO) that is not completely treated in the low temperature aqueous gasification reactor (LTS) at the end of the low temperature water gasification reactor (LTS). The carbon monoxide remover includes a selective oxidation unit (PROX), which receives air from an air supply unit and burns only the carbon monoxide (CO) in the gas discharged from the low temperature aqueous gasification reactor (LTS) H ₂ ) to reduce the concentration thereof.

The selective oxidation reactor (PROX) is equipped with a cooler and a temperature sensor. When the fuel cell system 200 according to an embodiment of the present invention includes the controller 250 (shown in FIG. 2), the controller 250 controls the cooler using a signal output from the temperature sensor The temperature of the selective oxidation reactor (PROX) is controlled. For example, the selective oxidation reactor (PROX) is controlled within the range of 120 to 160 占 폚. However, the optimal temperature of the selective oxidation reactor (PROX) is set differently depending on conditions such as the type of catalyst used and the method of use.

The catalyst layer of the selective oxidation reactor (PROX) comprises a structure filled with a carrier for supporting a selective oxidation catalyst. The selective oxidation catalyst is made of platinum (Pt) or the like, and the shape of the support carrying the catalyst may be, for example, a granular shape, a pellet shape, a honeycomb shape, etc. The material constituting the support may be alumina (Al ₂ O ₃ ) , Magnesium oxide (MgO), and the like.

Hereinafter, a fuel cell system 200 according to a second embodiment of the present invention will be described in detail with reference to the accompanying drawings.

5 is a conceptual configuration diagram of a fuel cell system according to a second embodiment of the present invention. 1 to 4, the same reference numerals are used.

Referring to FIG. 5, the fuel cell system 200 according to the second embodiment of the present invention includes a fuel cell 210, a hydrogen generator 400, and a heat exchanger 500. The fuel cell system 200 according to the present invention includes a control unit 250 for controlling operations of all the components including the fuel cell 210, the hydrogen generating unit 400, and the heat exchanging unit 500 .

The fuel cell 210 may include one or more fuel cell modules. The fuel cell 210 is supplied with the hydrogen-containing fuel from the hydrogen generator 400 and can generate electricity through an electrochemical reaction. The fuel cell 210 may be an alkaline fuel cell (AFC), a phosphoric acid fuel cell (PAFC), a molten carbonate fuel cell (MCFC), a solid oxide fuel cell (SOFC), a polymer electrolyte fuel cell (PEMFC) And a battery (DMFC).

The hydrogen generator 400 may include a raw material processing unit 410, a raw water treatment unit 420, a reformer 430, and a combustor 440. The hydrogen generating unit 400 receives LNG from the raw material supplying unit 110 and supplies water from the raw water supplying unit 120 to generate fuel containing hydrogen necessary for the fuel cell 210. The hydrogen generator 400 may discharge the waste heat generated in the process of generating hydrogen and the waste heat discharged from the fuel cell 210 to the heat exchanger 500. Accordingly, the heat exchanging unit 500 may be configured to heat the waste heat by a heat source for vaporizing the LNG, a heat source for increasing the amount of steam (H ₂ O), a heat source for heating the air supplied to the fuel cell 210 Can be used. Although not shown, the hydrogen generator 400 may include the aqueous gasification reactor 450 to lower the CO concentration of the fuel supplied to the fuel cell 210.

The heat exchanging unit 500 is connected to the high-temperature exhaust gas discharged from the hydrogen generating unit 400 so that the steam H ₂ 0 supplied from the raw water treating unit 420 is heated, The steam H ₂ 0 can be heat-exchanged. In this case, steam (H ₂ 0) that has passed through the heat exchanging unit 500 can be used as a heat source to be supplied to the raw material processing unit 410 to vaporize the raw material. For example, the steam (H ₂ 0) passed through the heat exchanging unit 500 is supplied to the LNG evaporator 410 (shown in FIG. 7) to function as a heat source for vaporizing the LNG, Can be generated. In this case, if the fuel cell 210 is a solid oxide fuel cell (SOFC), the fuel cell 210 may receive not only hydrogen (H ₂ ) but also fuel containing other gases such as carbon monoxide (CO) . The steam (H ₂ 0) passing through the heat exchanging part 500 may also be used as a heat source for vaporizing the LNG to supply fuel to the gas engine 600.

The heat exchange unit 500 of steam passed through the exhaust gas and the raw material processing unit 410 of a high temperature discharged from the fuel cell 210 to heat the steam (H ₂ 0) subjected to the material processing unit 410 (H ₂ 0) can be exchanged. In this case, the steam H ₂ 0 passing through the heat exchanging unit 500 can serve as a heat source for increasing the amount of the steam H ₂ 0 supplied to the raw water treatment unit 420. The heat exchanging unit 500 may heat-exchange the high-temperature exhaust gas discharged from the combustor 440 with the air so that the air supplied to the fuel cell 210 is heated. In this case, the air passing through the heat exchanging unit 500 can appropriately maintain the operating temperature of the fuel cell 210 so that the fuel cell 210 efficiently generates electricity. The heat exchanging unit 500 may include a first heat exchanging unit 510, a second heat exchanging unit 520, and a third heat exchanging unit 530, which perform the functions as described above.

FIGS. 6 and 7 are block diagrams of the fuel cell system of FIG. 5 according to the first embodiment.

Referring to FIGS. 6 and 7, the first embodiment of the fuel cell system 200 of the present invention includes the first heat exchanger 510.

The first heat exchanger 510 exchanges heat between the steam H ₂ 0 supplied from the raw water water processor 420 and the exhaust gas discharged from the combustor 440. In this case, the exhaust gas discharged from the combustor 440 becomes a heat source for heating the steam H ₂ 0 supplied from the raw water treatment unit 420. The high temperature steam H ₂ 0 passing through the first heat exchanging part 510 is supplied to the raw material processing part 400 of the hydrogen generating part 400 in which the fuel containing hydrogen supplied to the fuel cell 210 is generated, (Not shown) to the evaporator 410 to vaporize the raw material. Here, the raw water (H ₂ 0) supplied from the raw water treatment unit 420 may be supplied to the first heat exchange unit 510 by a pump or the like. In this case, the raw water treatment unit 420 may be a water separator 4201 for separating condensed water from steam (H ₂ O). The raw material treatment unit 410 may include an LNG evaporator 4101 for evaporating the raw material supplied from the LNG storage tank and a vaporizer 4102 installed in the LNG evaporator. Accordingly, the first heat exchanging unit 510 can exchange heat between the high temperature exhaust gas discharged from the combustor 440 and the steam H ₂ 0 supplied to the vaporizer 4102. The vaporizer 4102 can vaporize the LNG with the high-temperature steam (H ₂ 0) as a heat source. The vapor (H ₂ 0) in the vaporizer 4102 may be cooled after vaporizing the LNG, and may be transferred to the water separator 4201 through a pump or the like. The exhaust gas discharged from the combustor 440 passes through the first heat exchanging unit 510 and the condenser 4202 of the raw water treatment unit 420 while the water H ₂ 0 is supplied to the water separator 4201, and the remaining residual gas is discharged to the outside. The separator 4201 is a supply of water through the water of the water and steam supply to the steam (H ₂ 0) and then separating the (H ₂ 0) in the reformer 430, and the pump or the like in the (H ₂ 0) ( H ₂ 0) to the first heat exchanger 510.

Accordingly, in the first embodiment of the fuel cell system 200 of the present invention, the LNG is vaporized using the high-temperature exhaust gas discharged from the combustor 440 of the fuel cell 210 without a separate heating device, It not only improves the electricity production efficiency but also reduces the cost of constructing the electricity production. In addition, since the first embodiment of the fuel cell system 200 of the present invention does not require a separate heating device, it is easy to install even in a narrow space. Therefore, the first embodiment of the fuel cell system 200 of the present invention can increase the versatility of the installation space of the electric production apparatus.

Fig. 8 is a configuration diagram according to the second embodiment of the fuel cell system of Fig. 5; Fig. Referring to FIG. 8, the second embodiment of the fuel cell system 200 of the present invention further includes the second heat exchanger 520.

The second heat exchanger 520 wherein the material processing unit 410 via the steam (H ₂ 0) is passed through the exhaust gas and the raw material processing unit 410 is discharged from the fuel cell 210 to heat the steam (H ₂ 0). Here, the raw material processing unit 410 may be the vaporizer 4101. The steam (H ₂ 0) supplied to the vaporizer 4101 is vaporized by the vaporizer 4101 to cool the LNG, and some of the vapor is phase-changed into water. Accordingly, the amount of steam (H ₂ 0) subjected to the carburetor 4101 is reduced than the amount of steam (H ₂ 0) prior to go through the carburetor 4101. The amount of water separated by the water separator 4201 is increased when the amount of the steam H ₂ 0 that has passed through the vaporizer 4101 is reduced and the amount of water separated by the water separator 4201 is increased, The amount of steam H ₂ 0 to be supplied to the steam generator ₁ is reduced. Therefore, the water separator 4201 may be further loaded to generate steam (H ₂ O), and the efficiency of the fuel cell system 200 may be lowered. The second heat exchange unit 520 is steam (H ₂ 0) subjected to the carburetor 4101 so that the increased amount of steam (H ₂ 0) supplied to the separator 4201 in the carburetor 4101, and the Thereby exchanging heat at a high temperature exhaust gas discharged from the fuel cell 210. Thus, while passing through the carburetor 4101 is changed from the water steam (H ₂ 0) can be a phase change back to a steam (H ₂ 0) by the second heat exchanger (520). Here, the heat source in the second heat exchanging unit 520 is a high temperature exhaust gas discharged from the fuel cell 210.

Accordingly, the second embodiment of the fuel cell system 200 of the present invention increases the amount of steam (H ₂ 0) supplied from the vaporizer 4101 to the water separator 4201, 4201 may reduce the amount of water to be separated, thereby extending the service life of the water separator 4201. The second embodiment of the fuel cell system 200 of the present invention increases the amount of steam H ₂ 0 supplied to the water separator 4201 so that the steam H supplied to the reformer 430 ₂ 0 to increase the efficiency of the fuel cell system 200 by reducing the load of the water separator 4201. Although not shown, the second embodiment of the fuel cell system 200 of the present invention constructs a by-pass line without supplying the exhaust gas of the fuel cell 210 to the second heat exchanger 520 And is directly supplied to the combustor 440, whereby the same effect as that of the first embodiment can be achieved.

FIG. 9 is a configuration diagram of the fuel cell system of FIG. 5 according to the third embodiment. Referring to FIG. 9, the third embodiment of the fuel cell system 200 of the present invention further includes the air supply unit 130 and the third heat exchange unit 530.

The air supply unit 130 supplies air to the fuel cell 210. For example, the air supply unit 130 may supply external air to the fuel cell 210 through a blower or the like. The air supply unit 130 may supply air to the combustor 440 as well.

The third heat exchanging unit 530 is configured to heat the exhaust gas of the combustor 440 that has passed through the first heat exchanging unit 510 and the exhaust gas of the combustor 440 to heat the air supplied from the air supplying unit 130 to the fuel cell 210. [ Thereby exchanging heat with air supplied to the battery 210. The fuel cell 210 improves the electric production efficiency at an appropriate operating temperature. For example, in the case of a phosphoric acid type fuel cell (PAFC), the operation temperature is maintained at 190 to 210 ° C, the operation temperature of the MCFC is maintained at 550 to 650 ° C, In case of PEMFC, the operating temperature is maintained at 30 ~ 80 ℃. The third heat exchanging part 530 is connected to the exhaust gas of the combustor 440 and the fuel cell 210 through the first heat exchanging part 510 so as to improve the electricity production efficiency of the fuel cell 210. [ Exchanges the supplied air. In this case, the exhaust gas passing through the first heat exchanging part 510 becomes a heat source for heating the air supplied to the fuel cell 210. Although not shown, the control unit 250 may control the temperature of the air supplied to the fuel cell 210 by adjusting the amount of exhaust gas supplied to the third heat exchanging unit 530 through the by-pass line . For example, the control unit 250 increases the temperature of the air supplied to the fuel cell 210 by increasing the amount of the exhaust gas supplied to the third heat exchanging unit 530, thereby increasing the operating temperature of the fuel cell 210 It can be properly maintained. The control unit 250 decreases the amount of exhaust gas supplied to the third heat exchanging unit 530 so that the temperature of the air supplied to the fuel cell 210 is lowered to appropriately adjust the operating temperature of the fuel cell 210 . The control unit 250 may adjust the operation temperature of the fuel cell 210 by adjusting the amount of air supplied to the third heat exchanging unit 530.

Accordingly, the third embodiment of the fuel cell system 200 of the present invention is realized such that the fuel cell 210 maintains an appropriate operating temperature, thereby improving the electricity production efficiency, It is not necessary to separately provide a heating device for heating the supplied air, so that the installation cost of the heating device can be reduced.

FIG. 10 is a configuration diagram of the fuel cell system of FIG. 5 according to the fourth embodiment. 10, a fourth embodiment of the fuel cell system 200 of the present invention further includes a water separator 4201, an economizer 4203, a circulation unit 4204, and a gas engine 600.

The water separator 4201 separates moisture from steam (H ₂ 0). More specifically, the water separator 4201 separates moisture from steam (H ₂ 0) supplied from the vaporizer 4101. The water separator 4201 can separate water using a centrifugal separator, a metal net, a barrier plate, or the like. The water separated from the water separator 4201 may be discharged to the outside or may be supplied to the raw water supply unit 120. The steam H ₂ 0 separated by the water separator 4201 is circulated through the circulation unit 4204 between the water separator 4201 and the economizer 4203 or supplied to the reformer 430 , And can be used as a vaporization fluid for vaporizing LNG.

The economizer 4203 generates steam H ₂ 0 supplied to the raw material processing unit 410 and the water separator 4201 by using the high temperature exhaust gas discharged from the gas engine 600. The economizer 4203 is installed between the exhaust pipe of the gas engine 600 and the exhaust outlet. The economizer 4203 includes an inlet pipe, a high-pressure evaporator, an intermediate pipe, a low-pressure evaporator, and an outlet pipe. The inlet pipe is connected to the exhaust pipe of the gas engine 600 and guides the exhaust gas discharged from the gas engine 600 to the high-pressure evaporator. The intermediate pipe guides the exhaust gas after heat exchange in the high-pressure evaporator to the low-pressure evaporator. The outlet pipe guides the exhaust gas after heat exchange in the low pressure evaporator to the exhaust outlet. Accordingly, the fluid supplied from the water separator 4201 is heat-exchanged with the high temperature exhaust gas discharged from the gas engine 600 in the economizer 4203 to be phase-changed into steam H ₂ 0. Here, the fluid supplied from the water separator 4201 may be water. The steam H ₂ 0 generated through the economizer 4203 may be supplied to the vaporizer 4102 of the raw material processing unit 410 and the water separator 4201. The gas engine 600 generates propulsive force as fuel containing hydrogen generated in the raw material processing unit 410. Here, the hydrogen-containing fuel may be NG (natural gas) obtained by vaporizing LNG (liquefied natural gas). The NG (natural gas) may be vaporized in the vaporizer 4102 using steam (H ₂ O) passed through the first heat exchanger 510 as a heat source. The gas engine 600 is supplied with NG (natural gas) from the LNG evaporator 4101 to generate propulsive force by using the natural gas as fuel, and in this process, a high temperature exhaust gas is generated. The high-temperature exhaust gas may be a heat source supplied to the economizer 4203 to generate steam (H ₂ O).

The circulation unit 4204 circulates the fluid between the water separator 4201 and the economizer 4203 to recover heat from the exhaust gas discharged from the gas engine 600. The fluid may be water or steam (H ₂ 0). The circulation unit 4204 includes a pipe such as a pipe or a pipe connecting the water separator 4201 and the economizer 4203, and a pump installed in the pipe. The circulation unit 4204 supplies water to the economizer 4203 from the water separator 4201 and supplies steam H ₂ 0 from the economizer 4203 to the water separator 4201. That is, the circulation unit 4204 is configured to pass through the interior of the economizer 4203, so that the water supplied from the water separator 4201 is phase-changed into steam H ₂ 0, Can supply. Although not shown, a by-pass line may be installed in the return pipe circulating from the economizer 4203 to the water separator 4201 to use steam H ₂ 0 for other purposes.

Accordingly, the fourth embodiment of the fuel cell system 200 of the present invention further recovers heat from the waste heat of the exhaust gas discharged from the gas engine 600 to generate steam (H ₂ O) The installation cost of the device can be reduced and the amount of steam (H ₂ O) can be increased to increase the electricity production amount of the fuel cell 210.

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

11 is a schematic view showing an example of a ship according to the present invention.

Referring to FIGS. 1 to 11, a ship 900 according to the present invention is provided with a power generation system 100 on a ship 910. The power generation system 100 includes a fuel cell system 200. The fuel cell system 200 includes a fuel cell 210, a hydrogen generator 400, and a heat exchanger 500. The fuel cell system 200 may be implemented by including a controller for controlling operations of all the configurations including the fuel cell 210, the hydrogen generator 400, and the heat exchanger 500.

The fuel cell 210 may be an alkaline fuel cell (AFC), a phosphoric acid fuel cell (PAFC), a molten carbonate fuel cell (MCFC), a solid oxide fuel cell (SOFC), a polymer electrolyte fuel cell (PEMFC) And a battery (DMFC).

The hydrogen generator 400 may include a raw material processing unit 410, a raw water treatment unit 420, a reformer 430, and a combustor 440. The hydrogen generating unit 400 receives LNG from the raw material supplying unit 110 and supplies water from the raw water supplying unit 120 to generate fuel containing hydrogen necessary for the fuel cell 210. The hydrogen generator 400 may discharge the waste heat generated in the process of generating hydrogen and the exhaust gas discharged from the fuel cell 210 to the heat exchanger 500.

The heat exchanging unit 500 may include a first heat exchanging unit 510, a second heat exchanging unit 520, and a third heat exchanging unit 530. The first heat exchanging unit 510 can exchange heat between the high temperature exhaust gas discharged from the combustor 440 and the steam H ₂ 0 supplied from the water separator 4201. In this case, steam (H ₂ 0) passing through the heat exchanging part 510 can be used as a heat source to be supplied to the vaporizer 4102 to vaporize the LNG. Therefore, the fuel cell 210 can receive hydrogen-containing fuel from the LNG evaporator 4101. The hydrogen-containing fuel generated in the LNG evaporator 4101 may be supplied to the gas engine 600 and used as the fuel of the gas engine 600. The second heat exchanging unit 520 exchanges heat between the exhaust gas discharged from the fuel cell 210 and the steam H ₂ 0 passing through the vaporizer 4102. Accordingly, the second heat exchanging unit 520 can increase the amount of steam (H ₂ 0) supplied from the vaporizer 4102 to the water separator 4201. The third heat exchanging unit 530 exchanges heat between the exhaust gas of the combustor 440 and the air supplied to the fuel cell 210 through the first heat exchanging unit 510. Accordingly, the third heat exchanging unit 530 can maintain the proper operating temperature of the fuel cell 210 and improve the electricity production efficiency.

Accordingly, the ship 900 according to the present invention can achieve the following operational effects.

First, the ship 900 according to the present invention not only improves the electricity production efficiency by vaporizing the LNG using the high-temperature exhaust gas discharged from the combustor 440 of the fuel cell 210 without a separate heating device, The cost of constructing electricity production can be reduced.

Second, since the ship 900 according to the present invention does not require a separate heating device for obtaining the fuel necessary for producing electric power and the fuel required for propulsion, versatility for the installation space can be enhanced.

Third, the ship 900 according to the present invention increases the amount of steam (H ₂ 0) supplied from the vaporizer 4101 to the water separator 4201, so that the water separator 4201 can generate steam (H ₂ 0 Can be reduced. Accordingly, the marine vessel 900 according to the present invention can extend the service life of the water separator 4201, thereby reducing the operating cost consumed in the electricity production.

Fourth, since the ship 900 according to the present invention is configured to adjust the temperature of the air supplied to the fuel cell 210, the operation temperature of the fuel cell 210 can be appropriately maintained to improve the electricity production efficiency have.

Fifth, since the ship 900 according to the present invention is further configured to recover heat from the waste heat of the exhaust gas discharged from the gas engine 600, it is possible to reduce the installation cost of the heating apparatus, The efficiency of the fuel cell system 200 can be improved by increasing the amount of steam (H ₂ O) supplied.

Referring to FIGS. 1 to 11, the hull 910 constitutes the overall appearance of the ship 900 according to the present invention. The hull 910 is provided with an engine for generating a propulsive force for moving the hull 910 and a material supply unit 110 for supplying the material to the engine. For example, the raw material is a material of a hydrocarbon series, NG (natural gas), LPG (liquefied petroleum gas), methanol (CH ₃ OH), ethanol (C ₂ H ₅ OH), petrol, dimethyl ether, methane, hydrogen Liquid raw materials having a relatively high molecular weight such as refined off gas, pure water, and marine gas oil (MGO), marine diesel oil (MDO), and heavy fuel oil (HFO) .

The hull 910 is provided with a raw water supply part 120 for supplying the raw water necessary for the reforming reaction of the hydrogen generating part 400. The source water may be, for example, a constant, freshwater, or seawater. In another example, the raw water may be impurity removal treatment or ion removal treatment in a constant, fresh, or seawater.

The hull 910 is provided with an air supply unit 130 for supplying air to the fuel cell system 200. Normally, air means a gas including nitrogen, oxygen, carbon dioxide and the like, but also includes the case where nitrogen or carbon dioxide or both gases are removed from the air. The air supply unit 130 may include an air storage tank and a device (for example, a blower) for supplying air from the air storage tank. As another example, the air supply unit 130 may be configured to supply the compressed high-pressure air after compressing the external air.

A DC-DC converter for boosting or reducing the output voltage from the fuel cell system 200 and a DC-AC inverter for converting a direct current (DC) to an alternating current (AC) A conversion unit 140 is provided. The power conversion unit 140 discharges the electric power supplied from the fuel cell system 200 to the electric power load. The electric power load may be, for example, in-ship electrical equipment such as a ship's basic electrical equipment and cargo-system electrical equipment in the case of a ship. Although not shown, the power conversion unit 140 may be implemented to supply electricity to an energy storage device, for example, a battery.

In this specification, the term " ship " is not limited to a structure for navigating a watercraft, and includes not only a structure for navigating a watercraft, but also a floating oil production storage and unloading facility (FPSO) It includes the same sea structure.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, It will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the scope of the invention as defined by the appended claims. Accordingly, the true scope of the present invention should be determined only by the appended claims.

100: Power generation system
110: raw material supply part 120: raw material water supply part
130: air supply unit 140: power conversion unit
200: Fuel cell system
210: fuel cell 250:
400: hydrogen generator 500: heat exchanger
600: Gas engine

Claims (5)

As a vessel,
A raw material supply unit for supplying the raw material;
A raw water supply part for supplying raw water;
A fuel cell system for generating electricity using raw material supplied from the raw material supply unit and raw material water supplied from the raw water supply unit; And
And a power conversion unit for converting a direct current (DC) output from the fuel cell system into an alternating current (AC)
The fuel cell system includes:
A raw material supply unit for supplying a raw material to the raw material supply unit, a raw material supply unit for supplying the raw material supply source to the raw material supply unit, modifying the number of raw materials, including an economizer for generating steam (H ₂ 0) supplied to the raw material processing processor, a steam (H ₂ 0) supplied from the pre-processed fuel and the raw material can processing supplied from the raw material processing using A hydrogen generator including a reformer for reacting the reformer and a combustor for heating the reformer;
A fuel cell that generates electricity using fuel including hydrogen supplied from the hydrogen generator; And
And a first heat exchanger for exchanging heat between steam (H ₂ 0) supplied from the raw water water processor and exhaust gas discharged from the combustor,
The first heat exchanger is supplied with steam (H ₂ 0) discharged from the economizer,
The economizer further recovers heat from the waste heat of the exhaust gas discharged from the gas engine,
And the steam (H ₂ 0) routed through the first heat exchanger is used as a heat source supplied to the raw material treatment unit to vaporize the fuel. A raw material treatment section for pretreating the raw material supplied from the raw material supply section, an exhaust gas discharged from a gas engine that generates propulsion force as fuel containing hydrogen generated in the raw material treatment section for pretreating the raw water supplied from the raw water supply section A raw water treatment section including an economizer for generating steam (H ₂ 0) supplied to the raw material treatment section, a reforming reaction for the steam (H ₂ 0) supplied from the raw water treatment section and the pretreated fuel supplied from the raw material treatment section A hydrogen generator including a reformer and a combustor for heating the reformer;
A fuel cell that generates electricity using fuel including hydrogen supplied from the hydrogen generator; And
And a first heat exchanger for exchanging heat between steam (H ₂ 0) supplied from the raw water water processor and exhaust gas discharged from the combustor,
The first heat exchanger is supplied with steam (H ₂ 0) discharged from the economizer,
The economizer further recovers heat from the waste heat of the exhaust gas discharged from the gas engine,
And the steam (H ₂ 0) that has passed through the first heat exchanger is used as a heat source to be supplied to the raw material treatment unit and to vaporize the fuel. 3. The method of claim 2,
The so that the raw material processing via the steam (H ₂ 0) is heated, the fuel cell characterized in that it comprises a second heat exchange unit for heat exchange with the exhaust gas and steam (H ₂ 0) subjected to the material processing unit to be discharged from the fuel cell system. 3. The method of claim 2,
An air supply unit for supplying air to the fuel cell; And
And a third heat exchanger for exchanging heat between exhaust gas passing through the first heat exchanger and air supplied to the fuel cell so that air supplied to the fuel cell from the air supplier is heated. The water treatment system according to claim 2,
A water separator for separating moisture from steam (H ₂ O); And
And a circulation unit for circulating a fluid between the water separator and the economizer to recover heat from the exhaust gas discharged from the gas engine,
Wherein the economizer generates steam (H ₂ 0) supplied to the water separator using exhaust gas discharged from the gas engine.

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