KR101643103B1

KR101643103B1 - Ship

Info

Publication number: KR101643103B1
Application number: KR1020150120953A
Authority: KR
Inventors: 오태영
Original assignee: 현대중공업 주식회사
Priority date: 2015-08-27
Filing date: 2015-08-27
Publication date: 2016-07-28

Abstract

The present invention relates to a ship which is able to reduce construction costs, and increase space efficiency of installation spaces. To this end, the ship of the present invention comprises: a raw material supply unit for supplying raw materials; a raw water supply unit for supplying raw water; a fuel cell system which generates electricity by using the raw materials supplied from the raw material supply unit, and the raw water supplied from the raw water supply unit; and a power conversion unit which converts direct current (DC), outputted 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. The fuel cell can generate electricity by receiving fuel containing hydrogen from a reformer that reforms fuel and steam (H ₂ O). Reformer reforming a raw material, and the steam is heated by the combustor when supplied with steam (H ₂ 0) from the steam separator for separating water from (H ₂ 0) fuel and steam (H ₂ 0), such as NG (natural gas) .

Meanwhile, in the fuel cell system according to the related art, a separate heating device is installed to supply the raw material to the reformer that generates the fuel required for the fuel cell, thereby vaporizing the LNG. 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 electricity production efficiency is lowered because fuel or electric power must be supplied to a separate heating device for supplying heat for fuel generation used in the fuel cell.

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 problems, and it is an object of the present invention to provide a ship capable of reducing the construction cost and increasing the space utilization of 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 converter for converting a direct current (DC) output from the fuel cell system into an alternating current (AC), wherein the fuel cell system includes a hydrogen generator for generating fuel containing hydrogen, A first heat exchanger for supplying a fuel (H ₂ 0) used to produce electricity to the turbine, a fuel cell for generating electricity using the supplied fuel, a turbine for producing electricity, and a first heat exchanger The apparatus includes a raw material processing unit for pre-processing a raw material supplied from the raw material supply unit, a raw water water processing unit for pre-processing the raw water supplied from the raw water supply unit, a steam supplied from the raw material water processing unit, (H ₂ O), and a combustor for heating the reformer, wherein the raw material treatment section is a device for heating the reformer And an LNG evaporator for evaporating LNG using steam (H ₂ 0) for pretreating LNG as a raw material supplied from a raw material supply unit, wherein the raw water water processing unit includes a steam (H ₂ 0), and an economizer for heating the steam (H ₂ 0) supplied from the water separator, wherein the first heat exchanger comprises a steam (H ₂ 0) supplied from the economizer to the LNG evaporator H ₂ 0) and the exhaust gas discharged from the combustor, and the turbine generates electricity using steam (H ₂ 0) discharged from the first heat exchanger, and steam (H ₂ 0) used as a heat source to vaporize the LNG in the LNG evaporator, it said economizer heat is steam (H ₂ 0) to the waste heat of the exhaust gas exhausted from the gas engine as a heat source It may contain cyclic parts.
The vessel according to the present invention may include a second heat exchanger for exchanging heat between the LNG evaporator and the exhaust gas of the combustor discharged from the first heat exchanger, and water (H ₂ O) in the gaseous state discharged from the LNG evaporator .
A ship according to the present invention comprises: an air supply unit for supplying air to the fuel cell, the combustor, and the gas engine; And a third heat exchanging unit for exchanging heat between the steam (H ₂ 0) discharged from the economizer and the air supplied from the air supply unit so that the air supplied to the fuel cell and the combustor is heated.
The ship according to the present invention includes a fourth heat exchanger for exchanging heat between the steam (H ₂ 0) discharged from the turbine unit and the exhaust gas discharged from the fuel cell, and the steam heated by the fourth heat exchanger H ₂ O) may be supplied to the LNG evaporator.

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

The present invention is heated with steam (H ₂ 0) to the waste heat of the exhaust gas discharged from the waste heat and a burner exhaust gas exhausted from the gas engine by being implemented so as to vaporize the LNG, a separate heating using a conventional fuel or electric Without the device, LNG can be used for electricity production, which can improve the electricity production and the electricity production efficiency.

The present invention relates to a steam generator (H ₂ 0) generating device for supplying heat to an LNG evaporator by being implemented to heat steam (H ₂ 0) from waste heat of exhaust gas discharged from a gas engine and waste heat of exhaust gas discharged from a combustor, Since no separate heating device is required, it is possible to reduce the construction cost consumed for producing electricity and to increase 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 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, 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 is implemented including a diesel fuel storage tank and an apparatus 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 or ion-depleted water in fresh water or seawater. As another example, the raw water may be water in the state where impurities are removed from 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 that uses the combustion energy of the fuel.

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 ^-) 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 , &Lt; / 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 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. The raw material treatment unit 410 may include a filter for removing 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 treatment unit 420 generates steam (H ₂ O) by heating the raw water, and supplies the steam (H ₂ O) 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. As another example, the system may include an external water supply line and system for maintaining a certain level of water in the water supply unit 420.

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 reformed gas from the reformer 330 is defined as a 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 430 is adjusted by the conditions of the reformer 430 and the mixture ratio of the fuel pretreated in the raw material processing unit 410 and steam (H ₂ O) 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. When the fuel cell system 200 according to 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, (HTS) and the temperature of 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) has 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, FIGS. 6 and 7 are a configuration diagram according to the first embodiment of the fuel cell system of FIG. 5, Fig. 9 is a structural view of the fuel cell system according to the second embodiment, Fig. 9 is a configuration diagram according to the third embodiment of the fuel cell system of Fig. 5, and Fig. 10 is a schematic view of the fuel cell system of the fourth embodiment FIG. 1 to 4, the same reference numerals are used.

5 to 7, a fuel cell system 200 according to a second embodiment of the present invention includes a fuel cell 210, a hydrogen generator 400, a first heat exchanger 500, 600). The gas engine 1000 is installed to be connected to the hydrogen generator 400. The fuel cell system 200 according to the present invention includes all operations including the fuel cell 210, the hydrogen generating unit 400, the first heat exchanging unit 500, and the turbine unit 600 And a control unit 250 for controlling the control unit 250. [

Referring to FIGS. 5 to 7, the fuel cell 210 may supply fuel containing hydrogen from the hydrogen generator 400 to produce electricity through an electrochemical reaction. For example, the fuel cell 210 may receive fuel containing hydrogen from the reformer 430 and 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 fuel cell 210 can supply exhaust gas generated through an electrochemical reaction to the hydrogen generating unit 400. For example, the fuel cell 210 may supply a high temperature exhaust gas to the combustor 440 of the hydrogen generator 400.

5 to 7, 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.

Specifically, the raw material treatment unit 410 may include an LNG evaporator 4101 for evaporating the raw material supplied from the LNG storage tank of the raw material supply unit 110, and a vaporizer 4102 installed in the LNG evaporator .

The LNG evaporator 4101 may be supplied with NG (natural gas) which is naturally vaporized from the LNG storage tank 110 or LNG forcedly transported by a pump. The LNG evaporator 4101 is provided with the vaporizer 4102 therein, thereby vaporizing the LNG. The vaporizer 4102 vaporizes the LNG using the steam (H ₂ 0) generated in the raw water treatment unit 420 as a heat source. For example, the vaporizer 4102 can vaporize the LNG using the steam (H ₂ 0) supplied from the water separator 4201 of the raw water treatment unit 420 as a heat source. The steam H ₂ 0 supplied to the vaporizer 4102 from the water separator 4201 is firstly heated by the economizer 4203 of the raw water treatment unit 420 and is supplied to the first heat exchanger 500 As shown in Fig. The LNG evaporator 4101 is connected to the reformer 430, the combustor 440, and the gas engine 1000. Accordingly, the NG (natural gas) vaporized in the LNG evaporator 4101 is supplied to the reformer 430, the combustor 440, and the gas engine 1000 through an impeller, a blower, .

5 to 7, the raw water treatment unit 420 includes a water separator 4201 and an economizer 4203. [

The water separator 4201 separates moisture from steam (H ₂ 0). For example, the water separator 4201 supplies the water supplied from the raw water supply unit 120 to the economizer 4203 through a pump (not shown), circulates the water, and supplies the phase-changed steam H ₂ 0 It is possible to separate moisture. The water separator 4201 can separate water using a centrifugal separator, a metal net, a barrier plate, or the like. The water separated by the water separator 4201 may be discharged to the outside or may be supplied to the raw water supply unit 120 and stored. The steam H ₂ 0 discharged from the water separator 4201 may be heated by the economizer 4203 and supplied to the LNG evaporator 4101 and the reformer 430. 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.

The economizer 4203 heats the steam H ₂ 0 supplied from the water separator 4201. Here, the economizer 4203 can heat water or steam (H ₂ 0) supplied from the water separator 4201 using waste heat of the exhaust gas discharged from the gas engine 1000 as a heat source. The gas engine 1000 is installed to be connected to the LNG evaporator 4101 and may generate a driving force by receiving fuel including hydrogen generated from the LNG evaporator 4101. In this case, the hydrogen-containing fuel may be NG (natural gas) in which LNG is vaporized. Although not shown, the economizer 4203 is installed between the exhaust pipe of the gas engine 1000 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 an exhaust pipe of the gas engine 1000 and guides the exhaust gas discharged from the gas engine 1000 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 steam H ₂ 0 supplied from the water separator 4201 is heat-exchanged with the high-temperature exhaust gas discharged from the gas engine 1000 while passing through the high-pressure evaporator and the low-pressure evaporator. The steam (H ₂ 0) heat-exchanged in the economizer 4203 is supplied to the LNG evaporator 4101 and used as a heat source for vaporizing the LNG. The steam H ₂ 0 heated by the economizer 4203 is secondarily heated in the first heat exchanging unit 500 and then supplied to the LNG evaporator 4101 to vaporize the LNG. The second heated steam H ₂ 0 in the first heat exchanging unit 500 may be supplied to the reformer 430 and reformed to the NG gas supplied from the LNG evaporator 4101.

The economizer 4203 may further include a circulation unit 4203a. The circulation unit 4203a may include a pipe such as a pipe or a pipe, and an impeller, a pump, etc. installed in the pipe. The circulation unit 4203a is installed to be connected to the water separator 4201 and the economizer 4203. The cyclic portion (4203a) is a steam (H ₂ 0) is heated at the economizer 4203 supply water or steam (H ₂ 0) to, and the economizer (4203) the separator in the separator 4201 (4201). The water or steam H ₂ 0 supplied to the economizer 4203 by the circulation unit 4203a can be heated by the heat source as waste heat of the exhaust gas discharged from the gas engine 1000. Accordingly, steam (H ₂ 0) supplied from the economizer 4203 to the water separator 4201 through the circulation unit 4203 a can be used in the fuel cell system 200.

5 to 7, the first heat exchange unit 500 is installed between the LNG evaporator 4101 and the economizer 4203. [ The first heat exchanging unit 500 exchanges heat between exhaust gas discharged from the combustor 440 and steam (H ₂ O) supplied from the economizer 4203 to the LNG evaporator 4101. For example, the first heat exchanging unit 500 may include a channel through which steam (H ₂ O) flows from the economizer 4203 to the LNG evaporator 4101, and a channel through which the exhaust gas discharged from the combustor 440 flows The heat exchange can be performed. In this case, the waste heat of the exhaust gas discharged from the combustor 440 becomes a heat source for heating the steam (H ₂ O) supplied to the LNG evaporator 4101. Accordingly, the first heat exchanging unit 500 reduces the amount of residual moisture in the liquid state of the channel through which steam (H ₂ O) flows, and reduces the amount of steam (H ₂ O) supplied to the LNG evaporator 4101 . Further, in the first heat exchange unit 500 is steam (H ₂ O) supplied to being implemented to heat the economizer 4203 primary steam (H ₂ O) is heated in the second, LNG evaporator 4101 Temperature and pressure can be increased.

Referring to FIGS. 5 to 7, the turbine unit 600 is installed between the first heat exchanging unit 500 and the LNG evaporator 4101. The turbine unit 600 generates electricity using steam (H ₂ O) discharged from the first heat exchanging unit 500. For example, the turbine unit 600 may be a steam turbine. Although not shown, the turbine unit 600 may include a diaphragm, a rotor, a bucket, and a generator. The diaphragm is provided with a fixed blade, and the bucket is provided with a rotor blade. The fixed wick changes the direction of steam (H ₂ O) discharged from the first heat exchanging part (500) and guides the wick to the rotor blades. The rotor blade generates rotational force by steam (H ₂ O) Rotate the rotor. The rotor is installed to be connected to the generator. The generator can produce electricity as the rotor rotates. Accordingly, the turbine unit 600 can generate electricity using steam (H ₂ O) discharged from the first heat exchanging unit 500. The electricity generated by the turbine unit 600 may be supplied to an electric facility or an energy storage device, for example, a battery. The turbine section 600 changes the amount of electricity produced according to the pressure of steam (H ₂ O) supplied from the first heat exchanging section 500. For example, if the pressure of the steam (H ₂ O) supplied from the first heat exchanging part 500 is high, the turbine part 600 can rotate the rotor more quickly, thereby increasing the electric production amount. Steam (H ₂ O) passing through the turbine unit 600 is supplied to the LNG evaporator 4101 and used as a heat source for vaporizing the LNG.

Accordingly, the first embodiment of the fuel cell system 200 according to the present invention can achieve the following operational effects.

First, the first embodiment of the fuel cell system 200 according to the present invention uses the waste heat of the exhaust gas discharged from the gas engine 1000 and the waste heat of the exhaust gas discharged from the combustor 440, (H ₂ O) for vaporizing the LNG in the first heat exchanger 4101, it is possible to omit a separate heating device for supplying the heat source for vaporizing the LNG, thereby reducing the construction cost consumed for producing electricity .

Second, since the first embodiment of the fuel cell system 200 according to the present invention can omit a separate heating device for supplying a heat source for vaporizing the LNG, it is possible to supply the fuel supplied to the heating device to the fuel cell Therefore, it is possible not only to increase the electricity production amount but also to increase the versatility of the installation space.

In the first embodiment of the fuel cell system 200 according to the present invention, steam (H ₂ O) for vaporizing the LNG is firstly heated by the economizer 4203, and the first heat exchanger 500, The amount of steam (H ₂ O) supplied to the LNG evaporator 4101 can be increased as well as the temperature and pressure of steam (H ₂ O) can be increased. Accordingly, the first embodiment of the fuel cell system 200 according to the present invention can regulate the LNG vaporization rate in response to the increase / decrease of the load required for the power generation system 100, The amount of NG (natural gas) supplied to the gas engine 1000 can be quickly adjusted.

Fourth, in the first embodiment of the fuel cell system 200 according to the present invention, the turbine unit 600 is disposed between the first heat exchanging unit 500 and the LNG evaporator 4101, 210) can be additionally produced.

Referring to FIG. 8, the second embodiment of the fuel cell system 200 according to the present invention may further include a second heat exchange unit 700.

The second heat exchanger 700 is connected to the LNG evaporator 4101 through the exhaust gas from the combustor 440 discharged from the first heat exchanger 500 and the water (H ₂ O in liquid or gaseous state) Heat exchange is performed. The steam (H ₂ O) supplied to the LNG evaporator 4101 is vaporized by the LNG evaporator 4101 and is cooled to be phase-changed into water (H ₂ O as liquid or gaseous state). Steam (H ₂ O) passed through the LNG evaporator 4101 is supplied to the water separator 4201. In this case, since the water separator 4201 is supplied with steam (H ₂ O) having a high water content in a liquid state, the load for generating steam (H ₂ O) is increased and the efficiency of the water separator can do. Accordingly, the second heat exchanging unit 700 is installed in the exhaust port of the combustor 400 discharged from the first heat exchanging unit 500 so that the amount of steam (H ₂ O) supplied to the water separator 4201 increases, It is possible to heat the water (H ₂ O in liquid or gaseous state) discharged from the LNG evaporator 4101 using the waste heat of the gas as a heat source. Accordingly, the second embodiment of the fuel cell system 200 according to the present invention can reduce the amount of steam (H ₂ O) supplied to the water separator 4201 by setting the second heat exchanger 700 And the amount of water supplied to the water separator 4201 can be reduced. Therefore, the second embodiment of the fuel cell system 200 according to the present invention not only improves the efficiency of the water separator 4201 by reducing the load of the water separator 4201, but also extends the service life, It can reduce the cost of operation. In the second embodiment of the fuel cell system 200 according to the present invention, the amount of steam (H ₂ O) supplied to the water separator 4201 is increased so that the electricity production amount of the turbine unit 600 And can quickly cope with an increase in the LNG vaporization rate of the LNG evaporator 4101. The second heat exchanger 700 receives the water (H ₂ O in liquid or gaseous state) supplied from the LNG evaporator 4101 through the hot water tank 121 (shown in FIG. 7) It is also possible to use the waste heat of the exhaust gas of the combustor 400 discharged from the combustion chamber 500 to heat and supply the waste water to the water separator 4201. Although not shown, the raw water supply unit 120 may be connected to the hot water tank 121 to supply water required for the fuel cell system 200.

Referring to FIG. 9, the third embodiment of the fuel cell system 200 according to the present invention may further include an air supply unit 130 and a third heat exchange unit 800.

The air supply unit 130 is installed to supply air to the fuel cell 210, the combustor 440, and the gas engine 1000. Normally, air means a gas including nitrogen, oxygen, carbon dioxide and the like, but also includes the case where nitrogen or carbon dioxide or all gases other than oxygen 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 then supply compressed high-pressure air or atmospheric pressure.

The third heat exchanging unit 800 is installed between the economizer 4203 and the LNG evaporator 4101 and between the air supplying unit 130 and the fuel cell 210 and the combustor 440. The third heat exchanging unit 800 exchanges heat between steam (H ₂ O) discharged from the economizer 4203 and air supplied from the air supply unit 130. Accordingly, the third heat exchanging unit 800 may heat the 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 third heat exchanging unit 800 can supply the steam (H ₂ O) discharged from the economizer 4203 and the air supplied from the air supply unit 130 so that the electricity production efficiency of the fuel cell 210 can be improved. Heat exchange is performed. In this case, steam (H ₂ O) discharged from the economizer 4203 serves as a heat source for heating the air supplied to the fuel cell 210 and the combustor 440. Although not shown, the control unit 250 adjusts the amount of steam (H ₂ 0) supplied to the third heat exchanging unit 800 from the economizer 4203 so that the temperature of the air supplied to the fuel cell 210 Can be adjusted. For example, the control unit 250 increases the amount of steam (H ₂ 0) supplied to the third heat exchanging unit 800 to increase the temperature of the air supplied to the fuel cell 210, It is possible to increase the operating temperature. The control unit 250 reduces the amount of steam H ₂ 0 supplied to the second heat exchanging unit 700 so as to lower the temperature of the air supplied to the fuel cell 210 so that the operation of the fuel cell 210 Temperature can be lowered. The control unit 250 may adjust the operating temperature of the fuel cell 210 by adjusting the amount of air supplied to the third heat exchanging unit 800.

Accordingly, the third embodiment of the fuel cell system 200 according to the present invention can achieve the following operational effects.

The third embodiment of the fuel cell system 200 according to the present invention is configured to control the temperature of the air supplied to the fuel cell 210, It is possible to omit the heat source for the fuel cell 210, thereby improving the electricity production efficiency of the fuel cell 210.

Secondly, the third embodiment of the fuel cell system 200 according to the present invention is configured to heat the air supplied to the combustor 440, thereby reducing the heat loss generated by the combustion of the fuel in the combustor 440 The time for preheating the reformer 430 to a temperature required for the reforming reaction can be shortened.

Referring to FIG. 10, the fourth embodiment of the fuel cell system 200 according to the present invention may further include a fourth heat exchanging unit 810.

The fourth heat exchanging unit 810 is installed between the LNG evaporator 4101 and the turbine unit 600. The fourth heat exchanging unit 810 exchanges heat between exhaust gas discharged from the fuel cell 210 and steam (H ₂ O) supplied from the turbine unit 600 to the LNG evaporator 4101. For example, the fourth heat exchanging unit 810 may include a pipe through which steam (H ₂ O) flows from the turbine unit 600 to the LNG evaporator 4101, and a pipe through which the exhaust gas discharged from the fuel cell 210 flows The heat exchanging can be performed by bringing the conduit in close proximity. In this case, the waste heat of the exhaust gas discharged from the fuel cell 210 becomes a heat source for heating the steam (H ₂ O) supplied to the LNG evaporator 4101. Accordingly, the fourth heat exchanging unit 810 heats the steam (H ₂ O) whose temperature and pressure are lowered after generating power in the turbine unit 600, and the steam H (H) supplied to the LNG evaporator 4101 ₂ O) can increase the amount of steam (H ₂ O) by decreasing the amount of residual water in the liquid state of the channel in which it flows. A by-pass line may be provided in a conduit connecting the fuel cell 210 and the fourth heat exchanging unit 810 so that the exhaust gas of the fuel cell 210 is directly supplied to the combustor 440 It is possible.

Although not shown, the third embodiment including the second heat exchanging unit 700 and the third heat exchanging unit 800 may also include the fourth heat exchanging unit 810. Accordingly, even in the case of the second and third embodiments including the fourth heat exchanging unit 810, the temperature of the steam (H ₂ O) supplied from the turbine unit 600 to the LNG evaporator 4101 is increased .

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 and a gas engine 1000. The fuel cell system 200 includes a fuel cell 210, a hydrogen generator 400, a first heat exchanger 500, a turbine 600, a second heat exchanger 700, a third heat exchanger 800, And a fourth heat exchanging unit 810. The gas engine 1000 is installed to be connected to the hydrogen generator 400. The fuel cell system 200 includes the fuel cell 210, the hydrogen generator 400, the first heat exchanger 500, the turbine 600, the second heat exchanger 700, The third heat exchanging unit 800, the fourth heat exchanging unit 810, and the like.

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 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 4101, a condenser 4202, and an economizer 4203. [ The hydrogen generating unit 400 receives LNG from the raw material supplying unit 110 and supplies steam H ₂ 0 from the raw water supplying unit 120 to the fuel . At this time, the economizer 4203 can heat the steam (H ₂ 0) supplied to the LNG evaporator 4101 and the reformer 430 using the waste heat of the exhaust gas discharged from the gas engine 1000 have.

The first heat exchanging unit 500 exchanges heat between exhaust gas discharged from the combustor 440 and steam (H ₂ O) supplied from the economizer 4203 to the LNG evaporator 4101. In this case, the waste heat of the exhaust gas discharged from the combustor 440 becomes a heat source for heating the steam (H ₂ O) supplied to the LNG evaporator 4101. Accordingly, the first heat exchanging unit 500 can increase the amount of steam (H ₂ O) supplied to the LNG evaporator 4101. Further, in the first heat exchange unit 500 is steam (H ₂ O) supplied to being implemented to heat the economizer 4203 primary steam (H ₂ O) is heated in the second, LNG evaporator 4101 Temperature and pressure can be increased.

The turbine unit 600 generates electricity using steam (H ₂ O) discharged from the first heat exchanging unit 500. For example, the turbine unit 600 may be a steam turbine. The electricity generated by the turbine unit 600 may be supplied to an electric facility or an energy storage device, for example, a battery. Steam (H ₂ O) passing through the turbine unit 600 is supplied to the LNG evaporator 4101 and used as a heat source for vaporizing the LNG.

The second heat exchanger 700 is connected to the LNG evaporator 4101 through the exhaust gas from the combustor 440 discharged from the first heat exchanger 500 and the water (H ₂ O in liquid or gaseous state) Heat exchange is performed. In this case, the waste heat of the exhaust gas discharged from the combustor 440 becomes a heat source for heating the water (H ₂ O in liquid or gaseous state) discharged from the LNG evaporator 4101. Accordingly, the second embodiment of the fuel cell system 200 according to the present invention can increase the amount of steam (H ₂ O) supplied to the water separator 4201.

The third heat exchanging unit 800 heat-exchanges steam (H ₂ O) discharged from the economizer 4203 and air supplied from the air supply unit 130 to heat them. Accordingly, the third heat exchanging unit 800 can improve the electricity production efficiency of the fuel cell 210. The third heat exchanger 800 is configured to heat the air supplied to the combustor 440, thereby shortening the time for preheating the reformer 430 to a temperature required for the reforming reaction.

The fourth heat exchanging unit 810 exchanges heat between exhaust gas discharged from the fuel cell 210 and steam (H ₂ O) supplied from the turbine unit 600 to the LNG evaporator 4101. In this case, the waste heat of the exhaust gas discharged from the fuel cell 210 becomes a heat source for heating the steam (H ₂ O) supplied to the LNG evaporator 4101. Accordingly, the fourth heat exchanging unit 810 can increase the amount of steam (H ₂ O) supplied to the LNG evaporator 4101. Accordingly, the fourth heat exchanging unit 500 is required to heat steam (H ₂ O) having lowered temperature and pressure after power generation in the turbine unit 600 and to vaporize the LNG in the LNG evaporator 4101 Heat can be supplied.

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

First, the ship 900 according to the present invention uses steam (H ₂ O) to vaporize LNG using waste heat of the exhaust gas discharged from the gas engine 1000 and waste heat of the exhaust gas discharged from the combustor 440, It is possible to omit a separate heating device for vaporizing the LNG, so that the construction cost consumed for producing electricity can be reduced.

Second, since the ship 900 according to the present invention can omit a separate heating device for vaporizing the LNG, the fuel and electricity supplied to the heating device can be omitted, thereby increasing the electricity production efficiency, It is possible to increase the versatility of the space.

Third, the ship 900 according to the present invention may further generate electricity separately from the fuel cell 210 by disposing the turbine unit 600 between the first heat exchanging unit 500 and the LNG evaporator 4101 .

Fourth, the ship 900 according to the present invention is configured such that steam (H ₂ O) for vaporizing the LNG is firstly heated by the economizer 4203 and second heat is heated by the first heat exchanger 500, The amount of steam (H ₂ O) supplied to the LNG evaporator 4101 can be increased and the temperature of the steam (H ₂ O) can be increased. In addition, the ship 900 according to the present invention can generate steam (H ₂ O) having a sufficient temperature and pressure to generate electricity in the turbine unit 600.

Fifth, the ship 900 according to the present invention can reduce the load of the water separator 4201 by extending the service life of the water separator 4201 and increase the efficiency of the water separator 4201 by providing the second heat exchanger 700 have.

Sixth, the ship 900 according to the present invention is configured to adjust the temperature of the air supplied to the fuel cell 210 and the combustor 440 by installing the third heat exchanging unit 800, It is possible to improve the electricity production efficiency of the battery 210 and increase the combustion efficiency of the combustor 440.

Seventhly, the ship 900 according to the present invention is provided with the fourth heat exchanging unit 810 so that steam (H ₂ O) whose temperature and pressure are lowered after the power generation in the turbine unit 600 is supplied to the fuel cell 210, The temperature of the steam (H ₂ O) can be increased. Accordingly, the gasification rate of the LNG can be improved, so that it is possible to quickly supply NG (natural gas) to the reformer 430 and the gas engine 1000, as well as to control the supply amount of NG (natural gas).

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 oil (HFO) .

The hull 910 is provided with a raw water storage tank for storing raw water and a raw water supply unit 120 for supplying the raw water from the raw water storage tank. The raw water may be, for example, 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 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 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 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: first heat exchanger
600: turbine section 700: second heat exchange section
800: third heat exchanger 810: fourth heat exchanger
1000: Gas engine

Claims

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 hydrogen generator for generating a fuel containing hydrogen, a fuel cell for generating electricity using the fuel supplied from the hydrogen generator, a turbine for producing electricity, a first heat exchange unit comprises, for supplying the steam (H ₂ 0) which is used to
The hydrogen generator includes a raw material processing unit for pre-processing a raw material supplied from the raw material supply unit, a raw water water treatment unit for pre-treating the raw water supplied from the raw water supply unit, a pre-treated fuel supplied from the raw material treatment unit, A reformer for reforming the supplied steam (H ₂ O), and a combustor for heating the reformer,
The raw material processing unit includes an LNG evaporator for evaporating LNG using steam (H ₂ 0) to pretreat LNG as a raw material supplied from the raw material supply unit,
The raw water water treatment unit includes a water separator for separating moisture from steam (H ₂ 0) to pretreat raw water supplied from the raw water supply unit, and an economizer for heating steam (H ₂ 0) supplied from the water separator Including,
The first heat exchanger exchanges heat between steam (H ₂ 0) supplied from the economizer to the LNG evaporator and exhaust gas discharged from the combustor,
The turbine portion of the first, but generate electricity with steam (H ₂ 0) discharged from the heat exchange section, said turbine section via a steam (H ₂ 0) is used as a heat source to vaporize the LNG in the LNG evaporator,
The economiser vessel is characterized by comprising a cycle of heating the steam (H ₂ 0) to the waste heat of the exhaust gas exhausted from the gas engine as a heat source.

A hydrogen generator for generating a fuel containing hydrogen;
A fuel cell that generates electricity using fuel supplied from the hydrogen generator;
A turbine section for producing electricity;
Comprising a first heat exchange unit for supplying steam (H ₂ 0) which is used to produce electricity in the turbine section,
The hydrogen generator includes a raw material treatment section for pretreating the raw material supplied from the raw material supply section, a raw water treatment section for pretreating the raw water supplied from the raw water supply section, a preheated fuel supplied from the raw material treatment section, A reformer for reforming steam (H ₂ O), and a combustor for heating the reformer,
Wherein the raw material processing unit includes an LNG evaporator for evaporating LNG using steam (H ₂ 0) to pretreat LNG as a raw material supplied from the raw material supply unit,
The raw water water treatment unit includes a water separator for separating moisture from steam (H ₂ 0) to pretreat raw water supplied from the raw water supply unit, and an economizer for heating steam (H ₂ 0) supplied from the water separator &Lt; / RTI &
The first heat exchanger exchanges heat between steam (H ₂ 0) supplied from the economizer to the LNG evaporator and exhaust gas discharged from the combustor,
But the turbine section to produce electricity as steam (H ₂ 0) discharged from the first heat exchange section, said turbine section via a steam (H ₂ 0) is used as a heat source to vaporize the LNG in the LNG evaporator,
The economizer to the fuel cell system characterized in that it comprises a circulation of heating steam (H ₂ 0) to the waste heat of the exhaust gas exhausted from the gas engine as a heat source.

3. The method of claim 2,
A fuel cell system characterized in that it comprises a second heat exchange unit for heat exchanging the exhaust gas of the combustor, in which liquid or water (H ₂ O) as a gaseous phase discharged from the LNG evaporator, and discharged from the first heat exchange section.

3. The method of claim 2,
An air supply unit for supplying air to the fuel cell, the combustor, and the gas engine; And
And a third heat exchanger for exchanging heat between the steam (H ₂ 0) discharged from the economizer and the air supplied from the air supply unit so that the air supplied to the fuel cell and the combustor is heated.

3. The method of claim 2,
And a fourth heat exchanging unit for exchanging heat between steam (H ₂ 0) discharged from the turbine unit and exhaust gas discharged from the fuel cell,
Wherein the steam (H ₂ 0) which is heated in heat exchanger 4 is discharged to the fuel cell system being supplied to the LNG evaporator.