KR101704912B1 - Ship - Google Patents

Abstract

The present invention relates to a ship comprising: a raw material supply unit supplying raw materials; a raw water supply unit supplying raw water; a fuel cell system generating electricity by using the raw materials supplied from the raw material supply unit and raw water supplied from the raw water supply unit; and a power conversion unit converting direct current (DC), outputted from the fuel cell system, to alternative current (AC). According to the present invention, the ship can reduce installation costs and increase space availability.

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 required for 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 that the amount of electricity to be produced is reduced and the electricity production efficiency is lowered because the fuel is supplied to the fuel cell and the heating device separately or separately from the outside.

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 section 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 section for pre-processing a raw material supplied from a raw material supply section, A reformer for reforming steam (H ₂ 0) supplied from the raw water treatment section, and a combustor for heating the reformer, wherein the reformer is a reformer for reforming the raw water, A hydrogen generator; A fuel cell that generates electricity using fuel including hydrogen supplied from the hydrogen generator; And a heat exchange unit for exchanging heat between the vaporization fluid passing through the raw material treatment unit and the exhaust gas discharged from the combustor so that the vaporization fluid recovered by the raw water treatment unit is heated.
In the vessel according to the present invention, the raw water water treatment section may include an economizer for heating the air or the vaporization fluid with the exhaust gas discharged from the gas engine generating the propulsion force by the fuel containing the hydrogen generated in the raw material treatment section, And a water separator for separating moisture from the vaporizing fluid discharged from the economizer, wherein part of the vaporizing fluid recovers heat from the exhaust gas discharged from the gas engine while circulating between the water separator and the economizer, The economizer may heat the vaporization fluid supplied to the water separator in the heat exchange section.
In the vessel according to the present invention, the raw material treatment section includes an LNG evaporator for evaporating the raw material supplied from the LNG storage tank, and a vaporizer installed in the LNG evaporator, and the vaporizer is connected to the vaporizer through the economizer The fluid can be used as a heat source.
The vessel according to the present invention includes an air supply unit for supplying air to the fuel cell and the combustor, and the economizer can heat the air supplied to the fuel cell and the combustor from the air supply unit.

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

The present invention can be implemented to heat the vaporization fluid for vaporizing the LNG using the waste heat of the exhaust gas generated in the combustor, thereby improving the electric production amount and the electricity production efficiency.

The present invention is implemented to heat the vaporization fluid for vaporizing the LNG using the waste heat of the exhaust gas generated in the combustor, thereby reducing the construction cost consumed in producing electricity and increasing the versatility of the 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 according to an embodiment of the fuel cell system of FIG.
8 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, LNG (liquefied natural gas), LPG (liquefied petroleum gas), methanol (CH ₃ OH), ethanol (C ₂ H ₅ OH), petrol, dimethyl ether, methane, Hydrogen purification off-gas, pure hydrogen, or 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. In another example, the raw water may be impurity removal treatment or ion removal treatment in a constant, fresh, 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 the present invention may be implemented by including a controller 250 for controlling all operations including the fuel cell 210, the hydrogen generator 400, and the like. 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 the 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 or a cathode fan, a fuel electrode fan, a cooling plate, or 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 0) and the 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 the 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 the waste heat of the exhaust gas 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, which 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.

FIG. 5 is a conceptual configuration diagram of a fuel cell system according to a second embodiment of the present invention, and FIGS. 6 and 7 are block diagrams according to an embodiment of the fuel cell system of FIG. 1 to 4, the same reference numerals are used.

5 to 7, 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 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 include one or more fuel cell modules. For example, 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 methanol fuel cell (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. Although not shown, the hydrogen generator 400 may include an aqueous gasification reactor 450 to lower the CO concentration of the fuel supplied to the fuel cell 210 from the reformer 430. 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. For example, the hydrogen generator 400 may discharge the high-temperature exhaust gas discharged from the combustor 440 in which the exhaust gas discharged from the fuel cell 210 is combusted, to the heat exchanger 500. Accordingly, the heat exchange unit 500 can exchange heat between the waste heat discharged from the combustor 440 and the vaporization fluid for vaporizing the LNG. Here, the vaporization fluid may be at least one of water and steam (H ₂ O). For example, when the above-mentioned vaporized liquid is water, when heating is steam (H ₂ 0). In this case, since the steam (H ₂ 0) absorbs heat, it can be a heat source capable of vaporizing LNG. When the vaporization fluid is steam (H ₂ O), it becomes water when cooled. The vaporization fluid may coexist with water and steam (H ₂ O).

The heat exchange unit 500 is installed between the raw material treatment unit 410 and the raw water treatment unit 420. The heat exchanging unit 500 exchanges heat between the vaporizing fluid passing through the raw material processing unit 410 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 vaporization fluid passing through the raw material treatment section 410. The vaporization fluid is supplied to the raw water treatment section 420 by vaporizing the raw material in the raw material treatment section 410. Here, the vaporization fluid may be steam (H ₂ O), and the raw material may be LNG. The vaporizing fluid supplied to the raw material processing unit 410 is cooled after the LNG is vaporized in the raw material processing unit 410 and discharged from the raw material processing unit 410. Accordingly, the amount of water in the vaporizing fluid passing through the raw material treatment section 410 may be larger than the amount of steam (H ₂ O). The heat exchanging unit 500 exchanges heat between a vaporizing fluid passing through the raw material treating unit 410 and a high temperature exhaust gas discharged from the combustor 440. Accordingly, the water cooled through the raw material treatment unit 410 is heated by the high-temperature exhaust gas discharged from the combustor 440 in the heat exchanging unit 500 and is phase-changed into steam (H ₂ O). Accordingly, the amount of steam (H ₂ O) in the vaporizing fluid passing through the heat exchanging part (500) becomes larger than the amount of water. The vaporizing fluid passing through the heat exchanging part (500) is supplied to the raw water treatment part (420). The raw material processing unit 410 may include an LNG evaporator 4101 and a vaporizer 4102. The raw water water treatment unit 420 may include a water separator 4201 and a condenser 4202. The water separator 4201 may be provided with an economizer 4203 connected thereto.

Accordingly, in the embodiment of the fuel cell system 200 of the present invention, the heat exchanging part 500 is positioned at the rear end of the raw material processing part 410, the LNG is vaporized in the raw material processing part 410, The fluid for heating can be heated. Accordingly, in the embodiment of the fuel cell system 200 of the present invention, the exhaust gas discharged from the raw material treatment unit 410 is heat-exchanged with the vaporization fluid cooled by the vaporizer 4102, and is supplied to the raw water treatment unit 420 It is possible to increase the amount of steam (H ₂ O) supplied and ultimately supply the heat source necessary for vaporizing the LNG in the raw material treatment section 410. In the embodiment of the fuel cell system 200 of the present invention, the raw material water treatment section 420 supplies the heat source necessary for vaporizing LNG in the raw material treatment section 410 without a separate heat supply device, 4201, and the efficiency of the fuel cell system 200 can be improved.

Therefore, the embodiment of the fuel cell system 200 of the present invention can achieve the following operational effects.

First, in the embodiment of the fuel cell system 200 of the present invention, the vaporizing fluid cooled while passing through the raw material treatment section 410 is heated using the waste heat of the combustor 440 to generate steam, which is a heat source for vaporizing the LNG (H ₂ O) can be increased, so that the electric production efficiency and the electric production amount can be improved.

Second, in the embodiment of the fuel cell system 200 of the present invention, the waste heat discharged from the combustor 440 is used to heat the cooled vaporizing fluid while passing through the raw material treatment section 410 without a separate heating device It is possible to reduce the construction cost consumed in producing electricity.

Third, in the embodiment of the fuel cell system 200 of the present invention, since a heating device capable of heating the vaporizing fluid passing through the raw material treatment section 410 is not separately required, the versatility of the installation space can be enhanced.

Referring to FIG. 5, the heat exchanger 500 may be connected to the controller 250. Although not shown, the control unit 250 controls the amount of the vaporizing fluid supplied to the heat exchanging unit 500 and the amount of exhaust gas of the combustor 440 supplied to the heat exchanging unit 500, The generation rate of steam (H ₂ 0) generated by the steam generator (H ₂ 0) can be controlled. For example, the control unit 250 controls the opening degree of a channel provided between the raw material processing unit 410 and the heat exchanging unit 500, thereby controlling the opening degree of the vaporizing fluid supplied from the raw material treating unit 410 to the heat exchanging unit 500 The amount can be adjusted. For example, the control unit 250 controls the amount of exhaust gas supplied to the heat exchanging unit 500 from the combustor 440 by adjusting the opening degree of a duct provided between the combustor 440 and the heat exchanging unit 500 It is possible. For example, the opening degree adjustment may be performed by a valve. The control unit 250 reduces the amount of the vaporizing fluid supplied to the heat exchanging unit 500 and increases the amount of the exhaust gas of the combustor 440 so that the steam H generated in the heat exchanging unit 500 ₂ 0) can be accelerated. The control unit 250 may increase the amount of the vaporizing fluid supplied to the heat exchanging unit 500 and reduce the amount of the exhaust gas of the combustor 440 so that the steam generated by the heat exchanging unit 500 ₂ 0) can be slowed down. Accordingly, the embodiment of the fuel cell system 200 of the present invention controls the generation rate of the steam (H ₂ 0) generated in the heat exchanging unit 500 to control the amount of LNG vaporized in the normal and emergency To the fuel cell system (200) and the gas engine (600). Therefore, the embodiment of the fuel cell system 200 of the present invention not only can increase the efficiency of the power generation system 100, but also can appropriately respond to the electricity production speed and the propulsion speed control of the gas engine 600.

6 and 7, the raw material processing 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.

The LNG evaporator 4101 can be supplied with LNG that is naturally vaporized from the LNG storage tank 110 or LNG forcedly transferred by a pump. The LNG evaporator 4101 includes the vaporizer 4102 therein to vaporize the LNG. The LNG evaporator 4101 is connected to the gas engine 600, the reformer 430, and the combustor 440. Accordingly, the fuel vaporized in the LNG evaporator 4101 may be supplied to the gas engine 600, the reformer 430, and the combustor 440 through an impeller, a blower, or the like.

The vaporizer 4102 vaporizes the LNG in the LNG evaporator 4101. The vaporizer 4102 can vaporize the LNG using the vaporizing fluid as a heat source. For example, the vaporizer 4102 can vaporize the LNG using the high-temperature steam (H ₂ 0) discharged from the economizer 4203 as a heat source. The vaporization fluid cooled through the vaporizer 4102 may be supplied to the heat exchange unit 500.

Referring to FIG. 7, the raw water treatment unit 420 may include a water separator 4201 and a condenser 4202. The water separator 4201 may be provided with an economizer 4203 connected thereto.

The water separator 4201 separates moisture from the vaporizing fluid discharged from the economizer 4203. 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. Accordingly, the vaporization fluid supplied to the water separator 4201 is discharged through the water separator 4201 into the separated water H ₂ 0. The steam H ₂ 0 passed through the water separator 4201 is supplied to the economizer 4203 through a pump or the like to be circulated (not shown), supplied to the reformer 430, or fed to the LNG evaporator 4101 Can be supplied. When the separator of steam (H ₂ 0) subjected to 4201 is supplied to the LNG evaporator (4101), steam (H ₂ 0) subjected to the separator 4201 is in fluid vaporization for vaporizing the LNG Can be used.

The condenser 4202 cools and condenses the steam (H ₂ 0). The condenser 4202 can cool and condense the steam (H ₂ 0) by a method such as water-cooling, air-cooling or evaporation. The condenser 4202 cools and condenses the steam H ₂ 0 from the exhaust gas of the combustor 440 supplied through the heat exchanging unit 500. The steam H ₂ 0 is cooled and changed into water while passing through the condenser 4202 and the phase change water is supplied to the economizer 4203 and is phase-changed again to steam H ₂ 0. The phase-change water can be supplied to the water separator 4201. The phase-change water may be directly supplied to the water separator 4201 from the condenser 4202. In this case, the condenser 4202 can supply water to the water separator 4201 separately from the raw water supply part 120. Therefore, the condenser 4202 can reduce the amount of water supplied from the raw water supply part 120, thereby reducing the resources consumed in the electricity production. The residual gas other than the condensed water in the exhaust gas supplied to the condenser 4202 may be discharged to the outside.

The economizer 4203 heats the air or the vaporization fluid with the exhaust gas discharged from the gas engine 600, which generates the propulsive force by the fuel containing the hydrogen generated in the material processing unit 410, as a heat source. Although not shown, the economizer 4203 is installed between the exhaust pipe of the gas engine 600 and the exhaust outlet. The economizer 4203 comprises an inlet tube, a high-pressure evaporator, an intermediate tube, a low-pressure evaporator, and an outlet tube. 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. The fluid supplied to the economizer 4203 is heat-exchanged with the high-temperature exhaust gas discharged from the gas engine 600 while passing through the high-pressure evaporator and the low-pressure evaporator.

For example, the economizer 4203 can heat the steam H ₂ 0 supplied from the water separator 4201. In this case, the superheated steam H ₂ 0 generated by the heater 4203 may be supplied to the vaporizer 4102. The vaporizer 4102 may use the superheated steam H ₂ 0 supplied from the economizer 4203 as a heat source for vaporizing the LNG. Accordingly, the embodiment of the fuel cell system 200 of the present invention can reduce the cost of constructing a separate heating device for vaporizing the LNG.

For example, the economizer 4203 may heat the steam H ₂ 0 supplied from the heat exchanger 500 to the water separator 4201. In addition, the economizer 4203 may heat water supplied from the condenser 4202 to the water separator 4201. In this case, the economizer 4203 can increase the amount of steam (H ₂ 0) supplied to the water separator 4201. The steam H ₂ 0 supplied to the water separator 4201 may be supplied to the vaporizer 4102 through the reformer 430 and the economizer 4203. The amount of steam (H ₂ 0) supplied to the reformer 430 and the amount of the raw material supplied from the LNG evaporator 4101 are controlled to generate a fuel containing hydrogen necessary for the variation of the load of the fuel cell 210 The amount of hydrogen supplied to the fuel cell 210 can be controlled. Accordingly, the embodiment of the fuel cell system 200 of the present invention can adjust the electric production amount of the fuel cell 210 according to the load. Although not shown, when the amount of steam (H ₂ 0) supplied to the vaporizer 4102 increases, since increasing the heat source to vaporize the LNG flow rate the amount of steam (H ₂ 0) supplied to the vaporizer 4102 The amount of hydrogen supplied to the fuel cell 210 and the amount of fuel supplied to the gas engine 600 can be adjusted. Accordingly, the embodiment of the fuel cell system 200 of the present invention not only increases the electricity production amount of the fuel cell 210, but also increases the propulsive force of the gas engine 600, Can be increased. Although not shown, a by-pass line may be installed in the recovery pipe circulating from the economizer 4203 to the water separator 4201 to use steam H ₂ 0 for other purposes.

For example, the economizer 4203 may heat the air supplied from the air supply unit 130 to the fuel cell 210 and the combustor 440. In this case, the economizer 4203 can increase the temperature of air supplied to the fuel cell 210 and the combustor 440. 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 ℃. Accordingly, the economizer 4203 can heat the air supplied to the fuel cell 210 to an appropriate operating temperature according to the fuel cell 210. Accordingly, the embodiment of the fuel cell system 200 of the present invention can improve the electricity production efficiency 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.

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

Referring to FIGS. 1 to 8, 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 250 that controls the operation of all the configurations including the fuel cell 210, the hydrogen generator 400 and the heat exchanger 500 have.

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 generates waste heat generated in the process of generating hydrogen, for example, waste heat of the exhaust gas discharged from the combustor 440 and waste heat of the exhaust gas discharged from the fuel cell 210, (500). ≪ / RTI >

The heat exchanging unit 500 exchanges heat between the vaporizing fluid passing through the vaporizer 4102 and the exhaust gas discharged from the combustor 440. In this case, the exhaust gas discharged from the combustor 400 becomes a heat source for heating the vaporization fluid passing through the vaporizer 4102. The vaporizing fluid passing through the heat exchanging unit 500 is supplied to the economizer 4203, heated once, and then supplied to the water separator 4201. The vaporization fluid supplied to the water separator 4201 is heated while passing through the economizer 4203 and then supplied to the vaporizer 4102. The vaporizer 4102 can vaporize the LNG with the vaporizing fluid passing through the economizer 4203 as a heat source. Here, the vaporization fluid may be steam (H ₂ O). The heat exchanger 500 exchanges heat between the vaporizing fluid passing through the vaporizer 4102 and the exhaust gas discharged from the combustor 440 so that the amount of steam H ₂ 0 for vaporizing the LNG is increased.

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

First, the ship 900 according to the present invention vaporizes the LNG using the high-temperature exhaust gas discharged from the combustor 440 without a separate heating device, thereby improving the electric production efficiency and reducing the cost of constructing the electric production can do.

Second, since the ship 900 according to the present invention does not require a separate heating device for vaporizing the LNG in order to obtain the fuel necessary for producing electricity 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 operating costs consumed in electricity production.

Fourth, the ship 900 according to the present invention is configured to regulate the production rate of the steam (H ₂ 0) for vaporizing the LNG, so that electricity can be rapidly generated in an emergency in which power is urgently required.

Fifth, the ship 900 according to the present invention is configured to recover heat from the waste heat of the exhaust gas discharged from the gas engine 600, thereby reducing the heat discharged to the outside, thereby producing environmentally-friendly electricity.

1 to 8, 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 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 the external air is supplied, compress the high-pressure air, or to remove the foreign air and supply the compressed air at a normal pressure.

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:
Material processing unit for pre-processing the raw material supplied from the raw material supply portion, a raw pre-processing of raw water supplied from the raw water supply processing, the number of the pre-processed fuel and the raw material supplied from the raw material processing of the steam supplied from the processing unit (H ₂ 0) And a combustor for heating the reformer, wherein the reformer comprises: a reformer for reforming the reformer;
A fuel cell that generates electricity using fuel including hydrogen supplied from the hydrogen generator; And
And a heat exchange unit for exchanging heat between the vaporizing fluid passing through the raw material treatment unit and the exhaust gas discharged from the combustor so that the vaporization fluid recovered by the raw water treatment unit is heated,
The raw water water treatment unit includes an economizer for heating the air or the vaporization fluid with the exhaust gas discharged from the gas engine generating the propulsion force by the fuel containing the hydrogen generated in the raw material treatment unit as a heat source and the vaporizing fluid discharged from the economizer And a water separator for separating water from the water separator,
Wherein the economizer further heats the vaporization fluid supplied to the water separator in the heat exchange section. Material processing unit for pre-processing the raw material supplied from the raw material supply portion, a raw pre-processing of raw water supplied from the raw water supply processing, the number of the pre-processed fuel and the raw material supplied from the raw material processing of the steam supplied from the processing unit (H ₂ 0) And a combustor for heating the reformer, wherein the reformer comprises: a reformer for reforming the reformer;
A fuel cell that generates electricity using fuel including hydrogen supplied from the hydrogen generator; And
And a heat exchange unit for exchanging heat between the vaporizing fluid passing through the raw material treatment unit and the exhaust gas discharged from the combustor so that the vaporization fluid recovered by the raw water treatment unit is heated,
The raw water water treatment unit includes an economizer for heating the air or the vaporization fluid with the exhaust gas discharged from the gas engine generating the propulsion force by the fuel containing the hydrogen generated in the raw material treatment unit as a heat source and the vaporizing fluid discharged from the economizer And a water separator for separating water from the water separator,
Wherein the economizer further heats the vaporization fluid supplied from the heat exchange unit to the water separator. 3. The method of claim 2,
Wherein some of the vaporizing fluid circulates between the water separator and the economizer to recover heat from the exhaust gas discharged from the gas engine. The method of claim 3,
The raw material treatment unit includes an LNG evaporator for evaporating the raw material supplied from the LNG storage tank, and a vaporizer installed in the LNG evaporator,
Wherein the vaporizer uses the vaporization fluid passing through the economizer in the water separator as a heat source. 3. The method of claim 2,
And an air supply unit for supplying air to the fuel cell and the combustor,
Wherein the economizer heats air supplied to the fuel cell and the combustor from the air supply unit.

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