KR102190939B1 - Ship - Google Patents

Abstract

The present invention provides a raw material supply unit for supplying LNG (liquefied natural gas), a raw material water supply unit for supplying raw material water, a gas engine generating propulsion, and an economizer that uses waste heat of exhaust gas discharged from the gas engine as a heat source. A gas engine system including, a Rankine Cycle system that generates electricity using a refrigerant, a fuel cell system that generates electricity in connection with the gas engine system and the Rankine cycle system, and the fuel cell system It relates to a ship including a power converter for converting a direct current (DC) into an 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. In order to solve the problems associated with the use of fossil fuels, an environment-friendly power generation system is being developed.

Environmentally friendly power generation systems include power generation systems that generate electricity by converting renewable energy including sunlight, water, geothermal heat, precipitation, and biological organisms. In addition, environmentally friendly power generation systems include fuel cell systems that convert fossil fuels or generate electricity through chemical reactions such as hydrogen and oxygen.

Depending on the type of electrolyte used, fuel cells include alkaline fuel cells (AFCs), phosphoric acid fuel cells (PAFCs), molten carbonate fuel cells (MCFCs), solid oxides. It is classified into fuel cells (SOFC, Solid Oxide Fuel Cell), Polymer Electrolyte Membrane Fuel Cell (PEMFC), and Direct Methanol Fuel Cell (DMFC). Each of these fuel cells operates based on fundamentally the same principle, but differs in operating temperature, electrolyte, power generation efficiency, and power generation performance. The fuel cell may generate electricity by receiving fuel containing hydrogen from a reformer for reforming fuel and steam (H ₂ 0) and receiving air from the outside. The combustor heats the reformer by burning the exhaust gas discharged from the fuel cell.

On the other hand, in trains, ships, industrial vehicles, etc., a power generation system that generates necessary power using an engine including a diesel engine, a gas engine, etc. is commonly used. However, the power generation system using an engine has a low thermal efficiency of 40-50%. Recently, in the industry, a power generation system by an engine using a Carnot cycle and a fuel cell system using an electrochemical reaction as an environment-friendly power generation system are used in combination to generate necessary power and respond to global environmental pollution regulations. We are working on a new way.

However, in the case of the conventional technology that combines the power generation system using the engine and the fuel cell system, separate heating such as the Rankine Cycle system to vaporize fuel such as LNG used in gas engines or fuel cells. Since a device is required, the following problems arise.

First, in the conventional heating apparatus, a separate refrigerant circulating within the cycle was used to heat with electricity or to utilize a Rankine Cycle system. Accordingly, in the related art, since fuel or electricity used in fuel cells and gas engines must be supplied to the heating device, the amount of electricity produced by the fuel cell decreases, the electricity production efficiency decreases, and the cost for operating the power generation system increases. there is a problem.

Second, in the conventional heating device, a separate heating device for heating the refrigerant in the Rankine Cycle system must be installed, so that the installation cost of the heating device increases. Accordingly, in the related art, there is a problem that the construction cost for producing electricity increases.

Third, the conventional heating device requires a separate heating device installation space for heating the refrigerant of the Rankine Cycle system. Therefore, there is a problem in that the space of other devices for producing and storing electricity becomes narrow due to the installation of a heating device in the related art.

The present invention was conceived to solve the above-described problems, and is to provide a ship capable of improving the efficiency of a power generation system and increasing the amount of electricity produced.

The present invention is to provide a ship that can reduce the construction cost for generating electricity and increase the utilization of the installation space.

In order to solve the problems as described above, the present invention may include the following configuration.

The ship according to the present invention includes a raw material supply unit for supplying LNG (liquefied natural gas); A raw material water supply unit for supplying raw material water; A gas engine system including a gas engine generating propulsion and an economizer using waste heat of exhaust gas discharged from the gas engine as a heat source; Rankine Cycle system for generating electricity using a refrigerant; A fuel cell system that generates electricity in connection with the gas engine system and the Rankine cycle system; And a power conversion unit for converting a direct current (DC) output from the fuel cell system into an alternating current (AC), wherein the fuel cell system includes LNG (liquefied natural gas) supplied from the raw material supply unit to pretreatment. A raw material processing unit including an LNG evaporator for vaporizing (liquefied natural gas), a raw material water treatment unit including a water separator for separating water from steam (H ₂ 0) to pretreat the raw material water supplied from the raw material water supply unit, the A hydrogen generation unit including a reformer for reforming the pretreated fuel supplied from the raw material processing unit and the steam (H ₂ 0) supplied from the raw material water processing unit, and a combustor for heating the reformer; A fuel cell for generating electricity based on fuel including hydrogen supplied from the hydrogen generating unit; And a first heat exchanger configured to heat exchange the refrigerant of the Rankine cycle system and the exhaust gas discharged from the combustor so that the refrigerant of the Rankine cycle system is heated using the exhaust gas discharged from the combustor as a heat source.

In the ship according to the present invention, the gas engine of the gas engine system may generate a propulsion force with fuel vaporized in the LNG evaporator.

In the ship according to the present invention, water or steam (H ₂ 0) separated by the water separator may be supplied to the gas engine system and heated.

In the ship according to the present invention, the LNG evaporator may vaporize LNG (liquefied natural gas) by using the refrigerant of the Rankine cycle system supplied from the first heat exchange unit as a heat source.

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

The present invention is implemented to heat the refrigerant used in the Rankine Cycle system using waste heat of exhaust gas discharged from the combustor, so that it can be used for electricity production without a separate heating device using conventional fuel or electricity. In addition to improving the electricity production amount and the electricity production efficiency, since the fuel supplied to the conventional heating device can be used for the gas engine, the operating distance can be increased.

The present invention is implemented to heat the refrigerant used in the Rankine Cycle system by using the waste heat of exhaust gas discharged from the combustor, so that a separate heating device can be omitted, thereby reducing the construction cost consumed to produce electricity. Not only can it be done, but it can also increase the utilization of the installation space.

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

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

1 is a conceptual configuration diagram of an entire system according to the present invention, FIG. 2 is a conceptual configuration diagram of a fuel cell system according to a first embodiment of the present invention, and FIGS. 3A and 3B are diagrams of a fuel cell used in the present invention. As an exemplary diagram for explaining the operation, FIG. 3A is a conceptual configuration diagram of a solid oxide fuel cell (SOFC), FIG. 3B is a conceptual configuration diagram of a polymer electrolyte fuel cell (PEMFC), and FIG. 4 is an embodiment of the present invention. It is an exemplary diagram for explaining the hydrogen generation unit according to.

Referring to FIG. 1, the fuel cell system 200 according to the present invention is applied to the power generation system 100 to generate electricity. Prior to describing the fuel cell system 200 according to the present invention, a first look at the power generation system 100 is as follows.

The power generation system 100 includes a raw material supply unit 110, a raw material water supply unit 120, a gas engine system 130, a Rankine Cycle system 140, a power conversion unit 150, and a power conversion unit 150 according to the present invention. And a fuel cell system 200.

The raw material supply unit 110 includes a raw material storage tank, and supplies raw materials from the raw material storage tank. For example, raw materials are hydrocarbon-based materials, such as LNG (liquefied natural gas), LPG (liquefied petroleum gas), methanol (CH ₃ OH), ethanol (C ₂ H ₅ OH), gasoline, dimethyl ether, methane gas, It may be hydrogen-purified off-gas, pure hydrogen, or the like.

For example, when the power generation system 100 is applied to a vehicle, the raw material supply unit 110 includes a gas storage tank and a device (eg, 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 raw material supply unit 110 includes an LNG storage tank and a device for providing boil-off gas generated from 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 includes a diesel fuel storage tank and a device for supplying diesel fuel from the diesel fuel storage tank.

The raw material water supply unit 120 may include a raw material water storage tank and a device (eg, a pump) for supplying raw material water from the raw material water storage tank. The raw material water may be, for example, fresh water, fresh water, or sea water. As another example, the raw material water may be water that has been treated to remove impurities or ion-removed from fresh water or sea water. As another example, the raw material water may be fresh water or water in which impurities have been removed from seawater.

The gas engine system 130 may be implemented by including the gas engine 1301 and the economizer 1302. The gas engine 1301 generates a driving force with fuel obtained by vaporizing LNG (liquefied natural gas) supplied from the fuel cell system 200. For example, the gas engine 1301 may be installed to be connected to the LNG evaporator 4101 (shown in FIG. 7) of the fuel cell system 200 to receive fuel vaporized from the LNG evaporator to generate a driving force. The LNG evaporator 4101 may vaporize LNG (liquefied natural gas) using the refrigerant of the Rankine cycle system 140 as a heat source. The exhaust gas discharged from the gas engine 1301 may be supplied to an economizer 1302 (shown in FIG. 7) of the gas engine system 130. The economizer 1302 may phase change water into steam (H ₂ 0) using the exhaust gas of the gas engine 1301 as a heat source.

The economizer 1302 heats steam (H ₂ 0) supplied from the water separator 4201. The water separator 4201 receives water from the raw material water supply unit 120. Here, the economizer 1302 may heat water or steam (H ₂ 0) supplied from the water separator 4201 using exhaust gas discharged from the gas engine 1301 (shown in FIG. 7) as a heat source. Although not shown, the economizer 1302 is installed between the exhaust pipe of the gas engine 1301 and the exhaust outlet. The economizer 1302 includes an inlet pipe, a high pressure evaporator, an intermediate pipe, a low pressure evaporator, and an outlet pipe. The inlet pipe is connected to the exhaust pipe of the gas engine 1301 to guide the exhaust gas discharged from the gas engine 1301 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. Steam (H ₂ 0) supplied from the water separator 4201 is heat-exchanged with the high-temperature exhaust gas discharged from the gas engine 1301 while passing through the high-pressure evaporator and the low-pressure evaporator. Steam (H ₂ 0) heated by the economizer 1302 may be supplied to the reformer 430. Accordingly, the reformer 430 may perform a reforming reaction of the steam (H ₂ 0) supplied from the economizer 1302 and the fuel supplied from the LNG evaporator 4101.

Rankine cycle is a cycle consisting of two adiabatic changes and two isostatic pressure changes, and refers to a refrigerant accompanied by a phase change of vapor and liquid. The Rankine cycle consists of adiabatic compression, isostatic heating, adiabatic compression and isostatic heat dissipation. To this end, the Rankine cycle system 140 includes a pump 141 for adiabatic compression of the refrigerant, a heater for isostatic heating the refrigerant compressed by the pump 141, and a compressor for adiabatic compression of the refrigerant heated in the heater. 142 and a condenser 143 for dissipating the refrigerant compressed by the compressor 142 at isostatic pressure. The compressor 142 may be installed to be connected to a generator G (shown in FIG. 7 ), and may provide a driving force for generating electricity to the generator G. The compressor 142 may generate a driving force with a refrigerant supplied from the heater. The compressed refrigerant supplied to the heater may be heated by waste heat of the exhaust gas of the combustor 440 supplied to the first heat exchange unit 500 (shown in FIG. 7) of the fuel cell system 200. That is, the heater of the Rankine cycle system 140 may be replaced with the first heat exchange unit 500 (shown in FIG. 7) of the fuel cell system 200. The condenser 143 may be installed inside the LNG evaporator 4101 (shown in FIG. 7) of the fuel cell system 200. Accordingly, the LNG evaporator 4101 (shown in FIG. 7) of the fuel cell system 200 uses the refrigerant supplied from the first heat exchange unit 500 (shown in FIG. 7) as a heat source. Can vaporize.

The power conversion unit 150 converts the direct current (DC) 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 for converting a DC current (DC) into an AC current (AC). It may be composed of an inverter or the like. The power conversion unit 150 discharges electricity supplied from the fuel cell system 200 according to the present invention as a power load. For example, in the case of a ship, the power load may be an electrical equipment in a ship such as basic electrical equipment of a ship and electric equipment of a cargo system. Although not shown, the power conversion unit 150 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 uses fuel, water (H ₂ O), and air to generate electricity. The fuel cell system 200 according to the present invention may be used in small structures such as homes or automobiles, and may be used in large structures such as ships. The fuel cell system 200 according to the present invention may be implemented to interlock with a diesel engine, a gas engine, a steam turbine, a gas turbine, or a Rankine Cycle using combustion energy of fuel.

Hereinafter, a 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 generator 400. The fuel cell system 200 according to the present invention may be implemented by including a control unit 250 that controls the operation of all components including the fuel cell 210 and the hydrogen generator 400. In the present specification, raw materials and raw material water flowing into the hydrogen generating unit 400 are defined as fuel, and what is generated in the hydrogen generating unit 400 and flowing into the fuel cell 210 is defined as fuel.

The fuel cell 210 is implemented including a fuel cell stack. In the fuel cell stack, an electrolyte layer is formed between a cathode and an anode, and a separator for supplying hydrogen, supplying air, and recovering heat is provided at the anode and cathode. It is composed of the installed unit cell modules connected in series as much as the required quantity.

The fuel cell 210 is a temperature sensor and a temperature maintenance device. That is, a heater, a cathode fan, an anode fan, and a cooling plate may be included. The temperature sensor senses the temperature of the fuel cell stack, the temperature of the cathode, and the temperature of the anode. The fuel cell may be heated by the heater to maintain a temperature required for operation. The cathode fan dissipates heat generated by the cathode of the fuel cell stack. The anode fan dissipates heat generated by an anode of the fuel cell stack. The cathode fan and the anode 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 or cathode fan and the anode fan using a signal output from a temperature sensor to control the fuel cell 210 ) To properly maintain the operating temperature. For example, the control unit 250 maintains the operating temperature at 190 to 210°C in the case of a phosphoric acid fuel cell (PAFC), and maintains the operation temperature at 550 to 650°C in the case of a molten carbonate fuel cell (MCFC), and In the case of an oxide fuel cell (SOFC), the operating temperature is maintained at 650-1000°C, and in the case of a polymer electrolyte fuel cell (PEMFC), the operating temperature is maintained at 30-80°C.

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

First, referring to FIG. 3A, in a solid oxide fuel cell (SOFC) 310, oxygen ions generated by a reduction reaction of oxygen in a cathode 311 are transferred through an electrolyte 312 to an anode 313. Go to. Fuel containing hydrogen (H ₂ ) is introduced from the anode 313, and oxygen ions (O ^2- ) and hydrogen (H ₂ ) moved to the anode 313 through the electrolyte 312 Reacts electrochemically to produce water (H ₂ 0) and electrons (e-). 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 includes electrochemical unreacted substances such as carbon monoxide (CO) and carbon dioxide (CO ₂ ), which may be included in the fuel supplied to the anode 313, and unreacted hydrogen (H _{2 ).} ) And the reaction product water (liquid or gaseous H ₂ 0). In addition, unreacted oxygen and nitrogen are discharged from the cathode 311 of the solid oxide fuel cell (SOFC) 310.

Referring to FIG. 3B, in a polymer electrolyte fuel cell (PEMFC) 320, hydrogen (H ₂ ) is generated as hydrogen ions (H ⁺ ) and electrons (e-) in the catalyst layer 322 formed on the anode 321. do. Hydrogen ions (H ⁺ ) move to the cathode 324 through the polymer membrane 323. In the polymer electrolyte fuel cell (PEMFC) 320, hydrogen ions (H ⁺ ) and oxygen (O ₂ ) react in the catalyst layer 325 formed on the cathode 324 to produce water (H ₂ 0). 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 substances such as unreacted hydrogen (H ₂ ) from the catalyst layer 322 of the anode 321. In addition, the polymer electrolyte fuel cell (PEMFC) 320 discharges unreacted oxygen and water (H ₂ 0) from the cathode 324.

In addition, in the molten carbonate fuel cell (MCFC), hydrogen (H ₂ ) and carbonate ions (CO ₃ ^2- ) react at the anode, resulting in water (H ₂ O), carbon dioxide (CO ₂ ), and electrons (e-). Is created. The generated carbon dioxide (CO ₂₎ is sent to the air electrode (cathode), and carbon dioxide (CO ₂₎ and oxygen (O ₂₎ to react at the air electrode (cathode) to produce carbonate ions (C0 _3- ^2). Carbonate ions (C0 _3- ²⁾ is moved to the fuel electrode (anode) through the electrolyte. In the molten carbonate fuel cell (MCFC), carbon dioxide (CO ₂ ) generated in the process of generating electricity may be circulated inside the fuel cell without discharging to the outside.

Referring to FIGS. 2 and 4, the hydrogen generation unit 400 includes a device for generating fuel, that is, hydrogen (H ₂ ) gas required for an anode of the fuel cell 210 by using a raw material. In the present specification, raw materials and raw water flowing into the hydrogen generating unit 400 are defined as fuel, and what is generated in the hydrogen generating unit 400 and flowing into the fuel cell 210 is defined as fuel.

The hydrogen generation unit 400 may be designed in various ways according to the type of the fuel cell 210 or to improve electricity generation efficiency. For example, when the fuel cell 210 is a molten carbonate fuel cell (MCFC) or a solid oxide fuel cell (SOFC), the hydrogen generation unit 400 may be implemented by including a reformer and a combustor. . As another example, when the fuel cell 210 is a phosphoric acid type fuel cell (PAFC) or a polymer electrolyte fuel cell (PEMFC), the hydrogen generating unit 400 includes a reformer and a combustor, as well as a water gas shift reactor. , WGS) may be further included.

The water gasification reactor (WGS) is a high temperature water gasification reactor (HTS, High-Temperature Shift Reactor), a medium temperature water gasification reactor (MTS, Mid-Temperature Shift Reactor), a low temperature water gasification reactor (LTS, Low-Temperature Shift Reactor), Or it may include a carbon monoxide remover. The carbon monoxide remover may include a selective oxidation reactor (Preferential Oxidation, PROX) for removing only carbon monoxide (CO) by burning, or a methanation reactor for reducing the concentration by reacting carbon monoxide (CO) with hydrogen (H ₂ ). .

In the fuel cell system 200 according to the present invention with reference to FIG. 4, an example of the hydrogen generation unit 400 will be described as follows.

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

The raw material processing unit 410 pre-processes raw materials supplied from a raw material supply unit including a raw material storage tank. For example, the raw material processing unit 410 may be implemented by including an LNG evaporator 4101 that evaporates the liquefied natural gas supplied from the LNG storage tank. If 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., the raw material processing unit ( 410) includes a heater that applies heat to marine gas oil (MGO), marine diesel oil (MDO), or general heavy oil (HFO), and a methanizer that generates methane (CH ₄ ) by catalytic reaction of the heated raw material. Can be implemented. In addition, the raw material processing unit 410 may include a filter for removing impurities contained in the raw material or a desulfurization device for removing sulfides.

The raw material water treatment unit 420 pre-treats the raw material water supplied from the raw material water supply unit 120 including a raw material water storage tank. The raw material water treatment unit 420 generates steam (H ₂ O) by heating the raw material water, for example, and supplies the steam (H ₂ O) to a reformer. The raw material water treatment unit 420 may include, for example, a heat exchanger that heats raw material water with waste heat of exhaust gas generated from the combustor 440. In addition, the raw material water treatment unit 420 may be implemented by including a steam separator for separating moisture (water droplets) contained in exhaust gas or steam of the fuel cell system. In addition, the raw material water treatment unit 420 may use activated carbon, a resin for removing ions, etc. to maintain the purity required by the fuel cell system, and may include a sensor and a control system for measuring the raw material water. As another example, the raw material water treatment unit 420 may include an external water supply line and system for maintaining a predetermined level of water.

The reformer 430 proceeds with a reforming reaction of the pretreated fuel supplied from the raw material processing unit 410 and the steam (H ₂ 0) supplied from the raw material water processing unit 420 to generate hydrogen (H ₂ ). It generates a reformed gas containing. In carrying out such a reforming reaction, the reformer 430 may use heat energy provided from the combustor 440. Hereinafter, in the present specification, the reformed gas emitted from the reformer 330 is defined as fuel.

The reformer 430 is implemented by including a reforming catalyst layer that triggers a reforming reaction. The reforming catalyst layer has a structure in which the reforming catalyst is filled with a catalyst supported on a carrier. The reforming catalyst is made of nickel (Ni), ruthenium (Ru), platinum (Pt), and the like, and the shape of the carrier supporting the catalyst may be, for example, a granular shape, a pellet shape, and a honeycomb shape, and the material constituting the support May be ceramic, heat-resistant metal, or the like, such as alumina (Al ₂ O ₃ ) or titania (TiO ₂ ).

In the fuel cell system 200 according to the present invention, the reformer 430 may be installed outside the fuel cell 210. In this case, the fuel cell 210 is implemented in an external reforming type. In the fuel cell system 200 according to the present invention, the reformer 430 may be installed in the form of a reforming catalyst layer inside the fuel cell 210. In this case, the fuel cell 210 is implemented in an internal reforming type.

The combustor 440 provides heat so that the reforming reaction proceeds smoothly in the reformer 430. When the reformer heating temperature by the combustor 440 is low, the reforming reaction due to the endothermic reaction of the reformer 430 does not proceed well, and moisture (water droplets) is generated in the reformer 430 . When the heating temperature of the combustor 440 is high, the catalytic activity of the reforming catalyst layer of the reformer 430 may decrease.

In order to improve the overall efficiency of the system, the combustor 440 includes raw materials pretreated by the raw material processing unit 410, exhaust gas discharged from an anode of the fuel cell stack of the fuel cell 210, or both. A mixture of can be used as 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 additionally use air discharged from a cathode of the fuel cell stack of the fuel cell 210.

Although not shown, the hydrogen generating unit 400 may further include one or more temperature sensors, and the temperature sensor detects the temperature of the reformer 430. The temperature of the reformer 430 is the optimum temperature depending on the configuration of the reformer 430 and the mixing ratio of the fuel and steam (H ₂ O) pretreated in the raw material processing unit 410 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 control unit 250 uses a signal output from a temperature sensor to determine the combustor 440. ) To control the temperature of the reformer 430 by increasing or decreasing the amount of raw material combustion. For example, the controller 250 may be implemented to control 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) and carbon dioxide (CO ₂ ). 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. Accordingly, in order to reduce the concentration of carbon monoxide (CO) to 10 to 20 ppm or less, the hydrogen generation unit 400 may further include a water gasification reactor (WGS) 450.

The water gasification reactor (WGS) 450 reacts carbon monoxide (CO) with steam (H ₂ 0) to produce carbon dioxide (CO ₂ ) and hydrogen (H ₂ ). The water gasification reactor (WGS) 450 may include a high temperature water gasification reactor (HTS) and a low temperature water gasification reactor (LTS) as shown in FIG. 4.

The optimum temperature of the high-temperature water gasification reactor (HTS) and the low-temperature water gasification reactor (LTS) depends on the type of catalyst used, and the composition of the discharged gas is determined by equilibrium of the control temperature. Although not shown in FIG. 4, a cooler and a temperature sensor may be installed in the high-temperature water gasification reactor HTS and the low-temperature water gasification reactor LTS, respectively. When the fuel cell system 200 according to the present invention includes a control unit 250 (shown in Fig. 2), the control unit 250 controls the cooler using a signal output from a temperature sensor to control the high-temperature water gasification reactor. (HTS) and the temperature of the low-temperature water gasification reactor (LTS) are controlled. For example, the high-temperature water gasification reactor (HTS) is controlled within the range of 300 to 430 °C, and the low temperature water gasification reactor (LTS) is controlled within the 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 has not been completely treated in the low-temperature water gasification reactor (LTS) after the low-temperature water gasification reactor (LTS). The carbon monoxide remover receives air from the air supply unit and converts carbon monoxide (CO) into hydrogen (Preferential Oxidation, PROX), or carbon monoxide (CO), which burns and removes only carbon monoxide (CO) among gases discharged from the low-temperature water gasification reactor (LTS). It may include a methanation reactor to reduce the concentration by reacting with H ₂ ).

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 control unit 250 (shown in FIG. 2), the control unit 250 controls the cooler using a signal output from a temperature sensor. Controls the temperature of the selective oxidation reactor (PROX). For example, the selective oxidation reactor (PROX) is controlled within the range of 120 ~ 160 ℃. However, the optimum 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 supporting a selective oxidation catalyst. The selective oxidation catalyst is made of platinum (Pt), etc., and the shape of the support supporting the catalyst may be, for example, a granular shape, a pellet shape, and a honeycomb shape, and the material constituting the support is, for example, alumina (Al ₂ O ₃ ). , Magnesium oxide (MgO), etc.

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

5 and 6 are a conceptual configuration diagram of a fuel cell system according to a second embodiment of the present invention, FIG. 7 is a configuration diagram of the fuel cell system of FIG. 5 according to a first embodiment, and FIG. 8 is A configuration diagram of a fuel cell system according to a second embodiment, FIG. 9 is a configuration diagram according to a third embodiment of the fuel cell system of FIG. 5, and FIG. 10 is a configuration diagram of a fourth embodiment of the fuel cell system of FIG. It is a configuration diagram according to. Here, the same configuration as in FIGS. 1 to 4 uses the same reference numerals.

5 and 6, the fuel cell system 200 according to the second embodiment of the present invention includes a fuel cell 210, a hydrogen generating unit 400, and a first heat exchange unit 500. Here, the first heat exchange unit 500 may replace a heater that heats the refrigerant of the Rankine cycle 140 under constant pressure. The fuel cell system 200 according to the present invention includes a control unit 250 for controlling the operation of all components including the fuel cell 210, the hydrogen generating unit 400, and the first heat exchange unit 500. It may be implemented including.

Referring to FIGS. 5 and 6, the fuel cell 210 may receive fuel containing hydrogen from the hydrogen generator 400 and generate 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 be composed of one or a plurality of fuel cell modules. For example, the fuel cell 210 includes an alkali 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 direct It may include at least one fuel cell among methanol fuel cells (DMFC). The fuel cell 210 may supply exhaust gas generated through an electrochemical reaction to the hydrogen generating unit 400. For example, the fuel cell 210 may supply exhaust gas to the combustor 440.

5 and 6, the hydrogen generation unit 400 may be implemented by including a raw material processing unit 410, a raw material water treatment unit 420, a reformer 430, and a combustor 440. The hydrogen generation unit 400 receives LNG (liquefied natural gas) from the raw material supply unit 110 and receives water from the raw material water supply unit 120 to provide a fuel containing hydrogen required for the fuel cell 210. Create The raw materials stored in the raw material storage tank are marine gas oil (MGO), marine diesel oil (MDO), general heavy oil (HFO), methanol, dimethyl ether (DME), liquefied petroleum gas (LPG) and LNG (liquefied natural gas). It is a liquid raw material such as. In the present specification, LNG (liquefied natural gas) may be vaporized and supplied to the reformer 430, the combustor 440, and the gas engine 1301 (shown in FIG. 7).

5 to 7, the raw material processing unit 410 may include an LNG evaporator 4101 for evaporating LNG (liquefied natural gas) supplied from the raw material supply unit 110 including the LNG storage tank.

The LNG evaporator 4101 receives LNG (liquefied natural gas) from the LNG storage tank through a pump or the like. The LNG evaporator 4101 may be supplied with naturally vaporized NG (natural gas) from the LNG storage tank or LNG forcibly transferred by a pump. The LNG evaporator 4101 may vaporize LNG (liquefied natural gas) by installing a heating device therein. In addition, a condenser 143 of the Rankine cycle system 140 may be installed inside the LNG evaporator 4101.

5 to 7, the raw material water treatment unit 420 receives raw material water (eg, water) from the raw material water supply unit 120 to pretreat the raw material water. The raw material water treatment unit 420 may include a water separator 4201 and a first condenser 4202. The water separator 4201 may be installed to be connected to the gas engine system 130 including the gas engine 1301 and the economizer 1302.

The water separator 4201 separates water from steam (H ₂ 0). For example, the water separator 4201 may circulate water supplied from the raw material water supply unit 120 to the economizer 1302 to receive phase-changed steam (H ₂ 0) to separate water. The water separator 4201 may separate moisture using a centrifuge, a metal mesh, a baffle 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 material water supply unit 120 and stored. Steam H ₂ 0 discharged from the water separator 4201 may be supplied to the economizer 1302. Although not shown, a by-pass line may be installed in the recovery pipe circulating from the economizer 1302 to the water separator 4201 to use steam (H ₂ 0) for other purposes.

The first condenser 4202 is installed to be connected to the combustor 440 and condenses steam (H ₂ 0) included in the exhaust gas discharged from the combustor 440. The first condenser 4202 may cool and condense the steam H ₂ 0 by a method such as a water cooling type, an air cooling type, or an evaporation type. Accordingly, the steam (H ₂ 0) included in the exhaust gas of the combustor 440 supplied to the first condenser 4202 is phase-changed into water. The first condenser 4202 is installed to be connected to the first heat exchange unit 500 (shown in FIG. 7) of the Rankine cycle system 140 to be described later, and may receive the exhaust gas of the combustor 440. Water condensed in the first condenser 4202 may be supplied to the water separator 4201. Residual gas other than water condensed in the first condenser 4202 may be discharged to the outside.

5 to 7, the reformer 430 performs a reforming reaction of the fuel supplied from the LNG evaporator 4101 and the steam (H ₂ 0) supplied from the economizer 1302 to generate hydrogen (H _{2 ).} ) To generate a reformed gas. In carrying out such a reforming reaction, the reformer 430 may use heat energy provided from the combustor 440. The reformer 430 wherein the economizer 1302 the steam by being supplied to the (H ₂ 0), steam (H ₂ 0), the fuel and steam (H ₂ 0), no additional heating device for generating heat in the reforming The reaction efficiency can be further improved. Accordingly, the fuel cell system 200 according to the second embodiment of the present invention is implemented to improve the reforming reaction efficiency of the reformer 430, thereby smoothly supplying fuel containing hydrogen to the fuel cell 210. I can.

5 to 7, the combustor 440 provides heat so that the reforming reaction proceeds smoothly in the reformer 430. When the heating temperature of the reformer by the combustor 440 is low, the reforming reaction by the endothermic reaction of the reformer 430 does not proceed well, and moisture (water droplets) may be generated in the reformer 430. When the heating temperature of the combustor 440 is high, the catalytic activity of the reforming catalyst layer of the reformer 430 may decrease. In order to improve the overall efficiency of the system, the combustor 440 includes raw materials pretreated by the raw material processing unit 410, exhaust gas discharged from an anode of the fuel cell stack of the fuel cell 210, or both. A mixture of can be used as fuel. The combustor 440 may use air supplied from an air supply unit 600 (shown in FIG. 7 ). In the fuel cell system 200 according to the second embodiment of the present invention, the combustor 440 may additionally use air discharged from a cathode of the fuel cell stack of the fuel cell 210.

5 to 7, the first heat exchange unit 500 heat-exchanges the refrigerant of the Rankine Cycle system 140 for vaporizing LNG using a refrigerant and exhaust gas discharged from the combustor 440. Here, the refrigerant may be water (H ₂ 0 as a liquid or gas), carbon dioxide (CO ₂ ), propane, butane, ethylene glycol, propylene glycol, or a mixture thereof. The first heat exchange unit 500 may replace the heater of the Rankine cycle system 140. Accordingly, in the present specification, the Rankine cycle system 140 and the fuel cell system 200 will be classified, and the first heat exchanger 500 will be described.

First, when described in the Rankine cycle system 140, the exhaust gas supplied from the combustor 440 to the first heat exchange unit 500 is a refrigerant of the Rankine cycle system 140, that is, water (liquid or gas). H ₂ 0) It becomes a heat source for heating. In this specification, it will be described based on water. Accordingly, the water (H ₂ 0 as a liquid or gas) supplied from the pump 141 to the first heat exchange unit 500 is caused by the exhaust gas of the combustor 440 from the first heat exchange unit 500. It can be heated and phase-changed into steam (H ₂ 0). Steam (H ₂ 0) discharged from the first heat exchange unit 500 may be supplied to the compressor 142 to generate a driving force in the compressor 142. The compressor 142 is installed to be connected to a generator (G, shown in FIG. 7), thereby providing the generated driving force to the generator. Accordingly, the generator (G, shown in FIG. 7) may generate electricity. The Rankine cycle system 140 is implemented to heat the refrigerant adiabatically compressed by the compressor 142 at the condenser 143 in the LNG evaporator 4101 to dissipate isostatic pressure, and operates as an LNG heating device to the LNG evaporator 4101 LNG (Liquefied Natural Gas) can be vaporized from

The LNG evaporator 4101 is installed to be connected to the reformer 430, the combustor 440, and the gas engine 1301. Accordingly, NG (natural gas) vaporized in the LNG evaporator 4101 is supplied to the reformer 430, the combustor 440 and the gas engine 1301 through an impeller, a blower, etc. Can be. The refrigerant of the Rankine cycle system 140 that has passed through the condenser 143 may be supplied to the first heat exchange unit 50 by the pump 141 to exchange heat with the exhaust gas of the combustor 440. .

Next, in the fuel cell system 200, the exhaust gas supplied from the combustor 440 to the first heat exchange unit 500 is a refrigerant of the Rankine cycle system 140, that is, water (liquid or gas). It is cooled by H ₂ 0). Accordingly, the exhaust gas discharged from the first heat exchange unit 500 is at a lower temperature than the exhaust gas supplied to the first heat exchange unit 500. The exhaust gas discharged from the first heat exchange unit 500 may be supplied to the second heat exchange unit 700 (shown in FIG. 8 ).

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 is implemented to heat the refrigerant of the Rankine cycle system 140 by using the waste heat of the exhaust gas discharged from the combustor 440. A separate heating device for heating the can be omitted. Accordingly, in the first embodiment of the fuel cell system 200 according to the present invention, the fuel or electricity supplied to the refrigerant heating device of the Rankine cycle system 140 is converted to the fuel cell 210 and the gas engine 1301. ), it is possible to increase the amount of electricity produced as well as increase the efficiency of the power generation system 100.

Second, the first embodiment of the fuel cell system 200 according to the present invention is implemented to heat the refrigerant of the Rankine cycle system 140 by using the waste heat of the exhaust gas discharged from the combustor 440. A separate heating device for heating the can be omitted. Accordingly, in the first embodiment of the fuel cell system 200 according to the present invention, not only can the construction cost consumed for generating electricity can be reduced, but also the utilization of the installation space can be increased.

Third, the first embodiment of the fuel cell system 200 according to the present invention is implemented to vaporize LNG (Liquefied Natural Gas) using the refrigerant of the Rankine Cycle System 140 as a heat source, and thus LNG (Liquefied Natural Gas) A separate heating device for vaporizing can be omitted. Accordingly, in the first embodiment of the fuel cell system 200 according to the present invention, fuel or electricity supplied to a heating device for vaporizing LNG (liquefied natural gas) is supplied to the fuel cell 210 and the gas engine ( 1301), it is possible not only to increase the amount of electricity produced, but also to increase the efficiency of the power generation system 100.

Fourth, 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 1301 as a heat source and uses steam (H ₂ 0) supplied to the reformer 430. By being implemented to generate, it is possible to improve the efficiency of the power generation system 100.

Referring to FIG. 8, a second embodiment of the fuel cell system 200 according to the present invention may include an air supply unit 600 and a second heat exchange unit 700.

The air supply unit 600 is installed to supply air to the fuel cell 210, the combustor 440, and the gas engine 1301. Typically, air refers to a gas including nitrogen, oxygen, carbon dioxide, and the like, but in the present specification, nitrogen, carbon dioxide, or all gases other than oxygen are removed from the air. The air supply unit 600 may include an air storage tank and a device (eg, a blower) for supplying air from the air storage tank. As another example, the air supply unit 600 may be implemented to receive external air, compress it, and then supply compressed high-pressure air or supply it at normal pressure.

The second heat exchange unit 700 is supplied from the exhaust gas of the combustor 440 and the air supply unit 600 discharged from the first heat exchange unit 500 so that the air supplied from the air supply unit 600 is heated. Heat exchanged air. In this case, the exhaust gas of the combustor 440 discharged from the first heat exchange unit 500 becomes a heat source for heating the air supplied from the air supply unit 600. Accordingly, the second heat exchange unit 700 may heat the air supplied to the fuel cell 210 and the combustor 440. The fuel cell 210 improves electricity production efficiency at an appropriate operating temperature. For example, in the case of a phosphoric acid fuel cell (PAFC), the operating temperature is maintained at 190 to 210°C, in the case of a molten carbonate fuel cell (MCFC), the operating temperature is maintained at 550 to 650°C. In this case, the operating temperature is maintained at 650~1000℃, and in the case of a polymer electrolyte fuel cell (PEMFC), the operating temperature is maintained at 30~80℃. Accordingly, the second heat exchange unit 700 may preheat the air supplied to the fuel cell 210 so that the fuel cell 210 quickly reaches an appropriate operating temperature. Although not shown, the control unit 250 controls the amount of exhaust gas of the combustor 440 supplied from the first heat exchange unit 500 to the second heat exchange unit 700 to be supplied to the fuel cell 210. You can adjust the air temperature. For example, the control unit 250 controls a valve installed in a pipe connecting the first heat exchange unit 500 and the second heat exchange unit 700 to control the opening of the pipe, thereby controlling the second heat exchange The amount of exhaust gas of the combustor 440 supplied to the unit 700 may be adjusted. The control unit 250 may increase the temperature of air supplied to the fuel cell 210 by increasing the amount of exhaust gas supplied to the second heat exchange unit 700 to supply the air to the fuel cell 210. The control unit 250 may reduce the temperature of air supplied to the fuel cell 210 by reducing the amount of exhaust gas supplied to the second heat exchange unit 700 and supply it to the fuel cell 210. The control unit 250 may adjust the temperature of the supplied air according to the operating temperature of the fuel cell 210 by adjusting the amount of air supplied to the second heat exchange unit 700.

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

First, the second embodiment of the fuel cell system 200 according to the present invention is implemented to control the temperature of air supplied to the fuel cell 210, thereby improving the electricity production efficiency of the fuel cell 210 I can make it.

Second, the second embodiment of the fuel cell system 200 according to the present invention is implemented to heat the air supplied to the combustor 440, so that the time for preheating to the temperature required for the reforming reaction in the reformer 430 is reduced. You can shorten it.

Referring to FIG. 9, a second embodiment of the fuel cell system 200 according to the present invention may include an air supply unit 600 and a third heat exchange unit 800. Since the air supply unit 600 is the same as described above, it will be omitted, and the third heat exchange unit 800 will be described in detail.

The third heat exchange unit 800 heats the exhaust gas discharged from the fuel cell 210 and the air supplied from the air supply unit 600 so that the air supplied from the air supply unit 600 is heated. In this case, the exhaust gas discharged from the fuel cell 210 becomes a heat source for heating the air supplied from the air supply unit 600. Accordingly, the third heat exchanger 800 may heat the air supplied to the fuel cell 210 and the combustor 440. Although not shown, the control unit 250 controls the amount of exhaust gas of the fuel cell 210 supplied from the fuel cell 210 to the third heat exchange unit 800, thereby controlling the air supplied to the fuel cell 210. You can adjust the temperature. For example, the control unit 250 controls a valve installed in a pipe connecting the fuel cell 210 and the third heat exchange unit 800 to adjust the opening of the pipe, so that the third heat exchange unit ( The amount of exhaust gas of the fuel cell 210 supplied to 800 may be adjusted. The control unit 250 may increase the temperature of the air supplied to the fuel cell 210 by increasing the amount of exhaust gas supplied to the third heat exchange unit 800 and supply it to the fuel cell 210. The control unit 250 may reduce the temperature of the air supplied to the fuel cell 210 by reducing the amount of exhaust gas supplied to the third heat exchange unit 800 and supply it to the fuel cell 210. The control unit 250 may adjust the temperature of the supplied air according to the operating temperature of the fuel cell 210 by adjusting the amount of air supplied to the third heat exchanger 800.

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

First, the third embodiment of the fuel cell system 200 according to the present invention is implemented to control the temperature of air supplied to the fuel cell 210, thereby improving the electricity production efficiency of the fuel cell 210 I can make it.

Second, the third embodiment of the fuel cell system 200 according to the present invention is implemented to heat the air supplied to the combustor 440, so that the time for preheating to the temperature required for the reforming reaction in the reformer 430 is reduced. You can shorten it.

Referring to FIG. 10, a fourth embodiment of the fuel cell system 200 according to the present invention may include a second condenser 810.

The second condenser 810 is installed between the third heat exchanger 800 and the brackish water separator 4201. The second condenser 810 condenses steam (H ₂ 0) included in the exhaust gas of the fuel cell 210 discharged from the third heat exchanger 800. The second condenser 810 may cool and condense the steam H ₂ 0 by a method such as a water cooling type, an air cooling type, or an evaporative type. Accordingly, the second condenser 810 may condense the steam H ₂ 0 included in the exhaust gas of the fuel cell 210 into water. The second condenser 810 may supply condensed water to the water separator 4201. The remaining gas other than the water condensed in the second condenser 810 is supplied to the combustor 440. Accordingly, the fourth embodiment of the fuel cell system 200 according to the present invention condenses steam (H ₂ 0) from the exhaust gas of the fuel cell 210 discharged from the third heat exchange unit 800 into water. As a result, water required to produce steam (H ₂ 0) required by the fuel cell system 200 can be reduced because it can be supplied to the water separator 4201. In addition, the fourth embodiment of the fuel cell system 200 according to the present invention is implemented so that the exhaust gas discharged from the second condenser 810 is supplied to the combustor 440 to be burned. By using residual materials for combustion, fuel efficiency of the fuel cell system 200 can be increased, and unreacted residual material emissions can be reduced, thereby contributing to environmental protection.

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

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

1 to 11, the ship 900 according to the present invention is a power generation system 100 is installed in the hull 910. The power generation system 100 includes a fuel cell system 200. The fuel cell system 200 includes a fuel cell 210, a hydrogen generation unit 400, a first heat exchange unit 500, an air supply unit 600, a second heat exchange unit 700, and a third heat exchange unit 800. And a second condenser 810. The fuel cell system 200 includes the fuel cell 210, the hydrogen generating unit 400, the first heat exchange unit 500, the air supply unit 600, the second heat exchange unit 700, and the second heat exchange unit 700. It may be implemented by including a control unit 250 that controls the operation of all components including the 3 heat exchange unit 800 and the second condenser 810.

The fuel cell 210 may receive fuel containing hydrogen from the hydrogen generator 400 and generate 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 includes an alkali 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 direct methanol fuel. It may be implemented by including at least one fuel cell among the cells DMFC.

The hydrogen generation unit 400 may be implemented by including a raw material processing unit 410, a raw material water treatment unit 420, a reformer 430, and a combustor 440. The raw material processing unit 410 includes an LNG evaporator 4101 that receives and pre-processes raw materials from the raw material supply unit 110. A condenser 143 of the Rankine cycle system 140 may be installed inside the LNG evaporator 4101. Accordingly, the LNG evaporator 4101 may vaporize LNG (liquefied natural gas) using steam (H ₂ 0) supplied to the condenser 143 of the Rankine cycle system 140 as a heat source. The raw material water treatment unit 420 is used to pre-treat the raw material water supplied from the raw material water supply unit 120 to a water separator 4201 that separates water from the steam (H ₂ 0) and the exhaust gas of the combustor 440. A first condenser 4202 for condensing the included steam (H ₂ 0) and reducing it to water may be included. Water (liquid or gaseous H ₂ O) supplied from the water separator 4201 may be supplied to the gas engine system 130 and heated by the economizer 1302. The hydrogen generation unit 400 receives raw materials from the raw material supply unit 110, and receives steam (H ₂ 0) from the raw material water supply unit 120 to provide a fuel containing hydrogen required for the fuel cell 210. Create Here, the economizer 1302 may heat steam (H ₂ 0) supplied from the water separator 4201 using waste heat of the exhaust gas discharged from the gas engine 1301 as a heat source. The reformer 430 may use steam (H ₂ 0) supplied from the economizer 1302 for a reforming reaction. The LNG evaporator 4101 may vaporize LNG (liquefied natural gas) using steam (H ₂ 0) supplied to the condenser 143 of the Rankine cycle system 140 as a heat source.

The first heat exchange unit 500 heat-exchanges the refrigerant of the Rankine cycle system 140 for vaporizing LNG using a refrigerant and exhaust gas discharged from the combustor 440. Here, the refrigerant may be water (H ₂ 0 as a liquid or gas), carbon dioxide, propane, ethylene glycol and propylene glycol, or a mixture thereof. In this specification, it will be described based on water. The first heat exchange unit 500 may replace the heater of the Rankine cycle system 140. First, when the first heat exchange unit 500 is described in the Rankine cycle system 140, the exhaust gas supplied from the combustor 440 to the first heat exchange unit 500 is It becomes a heat source for heating the refrigerant, that is, water (H ₂ O as a liquid or gas). Accordingly, the water (H ₂ 0 as a liquid or gas) supplied from the pump 141 to the first heat exchange unit 500 is caused by the exhaust gas of the combustor 440 from the first heat exchange unit 500. It can be heated and phase-changed into steam (H ₂ 0). Steam (H ₂ 0) discharged from the first heat exchange unit 500 is supplied to the compressor 142 and is adiabatic compressed by the compressor 142. The compressor 142 is installed to be connected to a generator (G, shown in FIG. 7), thereby providing the generated driving force to the generator. Accordingly, the generator (G, shown in FIG. 7) may generate electricity. Next, when the first heat exchange unit 500 is described in the fuel cell system 200, the exhaust gas supplied from the combustor 440 to the first heat exchange unit 500 is a refrigerant of the Rankine cycle 140 , That is, cooled by water (H ₂ 0 as a liquid or gas). Accordingly, the exhaust gas discharged from the first heat exchange unit 500 is at a lower temperature than the exhaust gas supplied to the first heat exchange unit 500. The exhaust gas discharged from the first heat exchange unit 500 may be supplied to the second heat exchange unit 700 (shown in FIG. 8 ).

The Rankine cycle system 140 is implemented to heat the refrigerant adiabatically compressed by the compressor 142 at the condenser 143 in the LNG evaporator 4101 to dissipate isostatic pressure, and operates as an LNG heating device to the LNG evaporator 4101 LNG (Liquefied Natural Gas) can be vaporized from

The air supply unit 600 is installed to supply air to the fuel cell 210, the combustor 440, and the gas engine 1301. The air supply unit 600 may supply air to the fuel cell 210 and the combustor 440 through the second heat exchange unit 700. Typically, air refers to a gas including nitrogen, oxygen, carbon dioxide, and the like, but in the present specification, nitrogen, carbon dioxide, or all gases other than oxygen are removed from the air. The air supply unit 600 may be implemented to receive external air, compress it, and then supply compressed high-pressure air or supply it at normal pressure.

The second heat exchange unit 700 is supplied from the exhaust gas of the combustor 440 and the air supply unit 600 discharged from the first heat exchange unit 500 so that the air supplied from the air supply unit 600 is heated. Heat exchanged air. In this case, the exhaust gas of the combustor 440 discharged from the first heat exchange unit 500 becomes a heat source for heating the air supplied from the air supply unit 600. Accordingly, the second heat exchange unit 700 may heat the air supplied to the fuel cell 210 and the combustor 440.

The third heat exchange unit 800 heats the exhaust gas discharged from the fuel cell 210 and the air supplied from the air supply unit 600 so that the air supplied from the air supply unit 600 is heated. In this case, the exhaust gas discharged from the fuel cell 210 becomes a heat source for heating the air supplied from the air supply unit 600. Accordingly, the third heat exchanger 800 may heat the air supplied to the fuel cell 210 and the combustor 440.

The second condenser 810 condenses steam (H ₂ 0) included in the exhaust gas of the fuel cell 210 discharged from the third heat exchanger 800. The second condenser 810 may cool and condense the steam H ₂ 0 by a method such as a water cooling type, an air cooling type, or an evaporative type. Accordingly, the second condenser 810 may condense the steam H ₂ 0 included in the exhaust gas of the fuel cell 210 into water. Water condensed in the second condenser 810 may be supplied to the water separator 4201. Residual gas other than water condensed in the second condenser 810 may be supplied to the combustor 440.

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

First, the ship 900 according to the present invention is implemented to heat the refrigerant of the Rankine cycle system 140 by using waste heat of the exhaust gas discharged from the combustor 440, so that a separate heating device for heating the refrigerant Can be omitted. Accordingly, the ship 900 according to the present invention can supply fuel supplied to the heating device to the fuel cell 210 and the gas engine 1301, thereby increasing the amount of electricity produced, as well as the gas engine 1301. Can increase the uptime of

Second, the ship 900 according to the present invention is implemented to heat the refrigerant of the Rankine Cycle system 140 by using waste heat of the exhaust gas discharged from the combustor 440, and thus a separate heating device for heating the refrigerant. Can be omitted. Accordingly, the ship 900 according to the present invention can not only reduce the construction cost consumed to produce electricity, but also increase the utilization of the installation space.

Third, the ship 900 according to the present invention is implemented to vaporize LNG (Liquefied Natural Gas) using the refrigerant of the Rankine Cycle System 140 as a heat source, and thus a separate heating device for vaporizing LNG (Liquefied Natural Gas). Omit or reduce the fuel or electricity used in the heating device. Accordingly, the ship 900 according to the present invention can supply fuel or electricity supplied to the heating device for vaporizing LNG (liquefied natural gas) to the fuel cell 210 and the gas engine 1301, thereby producing electricity. In addition, it is possible to increase the efficiency of the power generation system 100 and increase the operating time of the gas engine 1301.

Fourth, the ship 900 according to the present invention is implemented to heat the steam (H ₂ 0) supplied to the reformer 430 by using waste heat of the exhaust gas discharged from the gas engine 1301 as a heat source, so that the reformer ( Since a separate heating device for generating steam (H ₂ 0) for the reforming reaction of 430 may be omitted, the efficiency of the power generation system 100 may be improved.

Fifth, the ship 900 according to the present invention is implemented to control the temperature of the air supplied to the fuel cell 210, thereby improving the efficiency of electricity production of the fuel cell 210.

Sixth, the vessel 900 according to the present invention is implemented to heat the air supplied to the combustor 440, thereby reducing heat loss due to a combustion reaction in the combustor 440.

Seventh, since the ship 900 according to the present invention can condense steam (H ₂ 0) contained in the exhaust gas of the fuel cell 210 into water and supply it to the water separator 4201, the fuel cell system 200 ), the water required to produce the steam (H ₂ 0) required can be reduced.

Eighth, the ship 900 according to the present invention is implemented so that the exhaust gas discharged from the second condenser 810 is supplied to the combustor 440 to be burned, so that the unreacted residual material in the exhaust gas is used for combustion. It is possible to contribute to environmental protection by increasing the fuel efficiency of the fuel cell system 200 and reducing the amount of unreacted residual material.

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

A raw material water storage tank for storing raw material water and a raw material water supply unit 120 for supplying raw material water from the raw material water storage tank are installed in the hull 910. The raw material water may be, for example, fresh water, or sea water. As another example, the raw material water may be water subjected to impurity removal treatment or ion removal treatment from fresh water or sea water.

A gas engine 1301 is installed in the hull 910 to generate a propulsive force from fuel in which LNG (liquefied natural gas) supplied from the raw material processing unit 410 is vaporized. The raw material processing unit 410 may include an LNG evaporator 4101, and the LNG evaporator 4101 may receive LNG (liquefied natural gas) stored in the raw material supply unit 110. The gas engine 1301 may supply exhaust gas generated while generating a propulsion force to the economizer 1302.

The hull 910 includes a Rankine cycle system 140 for vaporizing LNG in the LNG evaporator 4101 by heating a refrigerant using the exhaust gas discharged from the combustor 440 of the fuel cell system 200 as a heat source. Installed. The Rankine cycle system 140 may vaporize LNG (liquefied natural gas) supplied to the LNG evaporator 411 by using the heated refrigerant. The Rankine cycle system 140 includes a pump 141 for adiabatic compression of a refrigerant, a heater for isostatic heating of the refrigerant discharged from the pump 141, and a compressor 142 for adiabatic compression of the refrigerant discharged from the heater. And a condenser 143 for dissipating the refrigerant discharged from the compressor 142 at isostatic pressure. In the present specification, the heater of the Rankine cycle system 140 may be replaced with a first heat exchange unit 500 (shown in FIG. 7) of the fuel cell system 200. The condenser 143 of the Rankine cycle system 140 is installed inside the LNG evaporator 4101 to receive a refrigerant heated by the first heat exchange unit 500 and increased in pressure from the compressor 142. have.

The hull 910 includes a DC-DC converter for boosting or reducing the output voltage from the fuel cell system 200 and a DC-AC inverter for converting DC current to AC current. The conversion unit 150 is installed. The power conversion unit 150 discharges electricity supplied from the fuel cell system 200 as a power load. For example, in the case of a ship, the power load may be an electrical equipment in a ship such as basic electrical equipment of a ship and electric equipment of a cargo system. Although not shown, the power conversion unit 150 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 mean a structure sailing on the water, as well as a structure that sails on the water, as well as a floating crude oil production storage and handling facility (FPSO) that floats on the water and performs work. Includes the same marine structure.

Until now, the present specification has been described with reference to the embodiments shown in the drawings so that those of ordinary skill in the art to which the present invention belongs can easily understand and reproduce the present invention. Those of ordinary skill in the art will understand that various modifications and equivalent other embodiments are possible from the embodiments of the present invention. Therefore, the true technical protection scope of the present invention should be determined only by the appended claims.

100: power generation system
110: raw material supply unit 120: raw material water supply unit
130: gas engine system
140: Rankine Cycle system
150: power conversion unit
200: fuel cell system
210: fuel cell 250: control unit
400: hydrogen generation unit 500: first heat exchange unit
600: air supply unit 700: second heat exchange unit
800: third heat exchange unit 810: second condenser

Claims (6)

As a ship,
A raw material supply unit for supplying LNG (liquefied natural gas);
A raw material water supply unit for supplying raw material water;
A gas engine system including a gas engine generating propulsion and an economizer using waste heat of exhaust gas discharged from the gas engine as a heat source;
Rankine Cycle system for generating electricity using a refrigerant;
A fuel cell system that generates electricity in connection with the gas engine system and the Rankine cycle system; And
Including a power conversion unit for converting the direct current (DC) output from the fuel cell system into an alternating current (AC),
The fuel cell system,
A raw material processing unit including an LNG evaporator for vaporizing LNG (liquefied natural gas) to pretreat LNG (liquefied natural gas) supplied from the raw material supply unit, and steam (H ₂₎ to pretreat the raw material water supplied from the raw material water supply unit A raw material water treatment unit including a water separator for separating water at 0), a reformer for reforming the pretreated fuel supplied from the raw material treatment unit and the steam (H ₂ 0) supplied from the raw material water treatment unit, and heating the reformer Hydrogen generation unit including a combustor for;
A fuel cell for generating electricity based on fuel including hydrogen supplied from the hydrogen generating unit; And
And a first heat exchange unit for exchanging heat exchange between the refrigerant of the Rankine cycle system and the exhaust gas discharged from the combustor so that the refrigerant of the Rankine cycle system is heated using exhaust gas discharged from the combustor as a heat source,
The gas engine of the gas engine system generates a driving force with fuel vaporized in the LNG evaporator,
Water or steam (H ₂ 0) separated in the water separator is supplied to the gas engine system and heated,
The LNG evaporator vaporizes LNG (liquefied natural gas) using a refrigerant of the Rankine cycle system supplied from the first heat exchange unit as a heat source,
Further comprising a first condenser for condensing the steam contained in the exhaust gas discharged from the combustor,
Wherein the first heat exchange unit replaces a heater for heating the refrigerant of the Rankine cycle system under constant pressure using exhaust gas discharged from the combustor and transferred to the first condenser. A raw material processing unit including an LNG evaporator that vaporizes LNG (liquefied natural gas) to pretreat LNG (liquefied natural gas) supplied from the raw material supply unit, and steam (H ₂ 0) to pretreat the raw material water supplied from the raw material water supply unit A raw material water treatment unit including a water separator for separating water from the raw material water treatment unit, a reformer for reforming the pretreated fuel supplied from the raw material treatment unit and the steam (H ₂ 0) supplied from the raw material water treatment unit, and for heating the reformer A hydrogen generation unit including a combustor;
A fuel cell for generating electricity based on fuel including hydrogen supplied from the hydrogen generating unit; And
Including a first heat exchange unit for heat exchange between the refrigerant of the Rankine cycle system and the exhaust gas discharged from the combustor so that the refrigerant of the Rankine Cycle system for vaporizing LNG using a refrigerant is heated using the exhaust gas discharged from the combustor as a heat source. and,
The water or steam (H ₂ 0) separated in the water separator is a fuel vaporized in the LNG evaporator and a gas engine that generates a thrust and an economizer that uses waste heat from exhaust gas discharged from the gas engine as a heat source. Is supplied to the engine system and heated,
The LNG evaporator vaporizes LNG (liquefied natural gas) using a refrigerant of the Rankine cycle system supplied from the first heat exchange unit as a heat source,
Further comprising a first condenser for condensing the steam contained in the exhaust gas discharged from the combustor,
And the first heat exchange unit replaces a heater for heating the refrigerant of the Rankine cycle system under constant pressure using exhaust gas discharged from the combustor and transferred to the first condenser. The method of claim 2,
The reformer is a fuel cell system, characterized in that the reforming reaction of the steam (H ₂ 0) supplied from the economizer and the fuel supplied from the LNG evaporator. The method of claim 3,
An air supply unit for supplying air to the fuel cell, the combustor, and the gas engine,
A fuel cell system comprising a second heat exchange unit configured to heat exchange the exhaust gas of the combustor discharged from the first heat exchange unit and air supplied from the air supply unit to heat the fuel cell and air supplied to the combustor. The method of claim 3,
An air supply unit for supplying air to the fuel cell, the combustor, and the gas engine,
A fuel cell system comprising a third heat exchanger configured to heat-exchange exhaust gas discharged from the fuel cell and air supplied from the air supply unit so that the air supplied to the fuel cell and the combustor is heated. The method of claim 5,
A second condenser installed between the third heat exchange unit and the water separator and configured to condense steam (H ₂ 0) included in the exhaust gas of the fuel cell discharged from the third heat exchange unit,
The fuel cell system, characterized in that water discharged from the second condenser is supplied to the water separator.

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